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1	CN202511707827	CN202511707827	CN121454002	117662153	CN121454002 A 2026-02-03 [CN121454002]	2025-11-20	2025-11-20	2026-02-03		(CN121454002)\|2045-11-20	(CN121454002)\|Leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions	(CN121454002)\|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, and belongs to the technical fields of rock weathering and carbon sequestration enhancement, mineral fertilizer development and saline soil improvement and treatment. The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions. The leaching equipment comprises a temperature control device, a leaching assembly, a rainfall simulation device, a temperature and humidity sensor and a controller, wherein the temperature control device comprises a support frame and a constant temperature box device arranged on the support frame. The leaching assembly comprises a leaching column arranged in the constant-temperature box device and a liquid collecting container arranged below the leaching column. The equipment can simulate a chemical weathering leaching experiment of silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment so as to really simulate a chemical weathering process of the silicate minerals in a natural environment of saline-alkali soil; scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners, novel mineral fertilizers and saline-alkali soil improvement.	LANZHOU UNIVERSITY\|MICROCARBON LOW CARBON TECHNOLOGY	(CN121454002)\|LANZHOU UNIVERSITY ([CN])\|Microcarbon (Guangzhou) Low Carbon Technology Co., Ltd.	ZHANG JIETANG\|LI XINGYUAN\|GOU XIAOHUA	(CN121454002)\|ZHANG JIETANG\|LI XINGYUAN\|GOU XIAOHUA	(CN121454002)\|HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP)\|Reg. Nb: 41028	(CN121454002)\|It will be appreciated that in some of these embodiments the first valve 9 and the second valve 10 are solenoid valves.\|The problems cause great deviation between laboratory simulated silicate mineral weathering experimental results and chemical weathering under actual natural conditions, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain.\|Based on the problem that the laboratory simulation silicate mineral weathering experimental result in the prior art has larger deviation from the chemical weathering under the actual natural condition, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain, the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions, which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable temperature and humidity conditions, so as to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and provide scientific basis and experimental support for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers.\|In practical researches, the following problems are common in the conventional silicate mineral chemical weathering leaching experimental device: (1) By adopting a manual liquid adding mode, the leaching solution amount is difficult to be matched with the natural precipitation condition;\|	(CN121454002)\|1. An leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, comprising: The temperature control device comprises a support frame and an incubator device arranged on the support frame; The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.\|	(CN121454002)\|In order to achieve the purpose, the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided, and comprises:\|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, and belongs to the technical fields of enhanced rock weathering carbon fixation, mineral fertilizer development and saline soil improvement and management.\|	(CN121454002)\|LEACHING COLUMN(100,88)\|POWDER(100,60)\|SILICATE(100,50)\|NATURAL TEMPERATURE(100,30)\|SIMULATING CHEMICAL WEATHERING(100,27)\|HUMIDITY CONDITION(100,16)\|LEACHING EQUIPMENT(100,7)\|SYNCHRONOUS PULLEY(77,6)\|RAINFALL SIMULATION(74,20)\|LINK ROD(71,15)\|LEACHING(65,36)\|INCUBATOR(54,39)\|CHEMICAL WEATHERING LEACHING EXPERIMENT(51,2)\|MULTIFUNCTIONAL SILICATE MINERAL DEVELOPMENT(49,3)\|LABORATORY SIMULATION SILICATE MINERAL(48,1)\|LEACHING EXPERIMENT(47,3)\|MULTIFUNCTIONAL SILICATE MINERAL(46,3)\|NUTRIENT RELEASE(44,2)\|HUMIDITY(41,34)\|RELIABLE SILICATE MINERAL(41,2)\|INJECTION CYLINDER(40,23)\|SIMULATED RAINFALL(39,5)\|COLUMNAR ROCK MASS(39,3)\|MINERAL FERTILIZER DEVELOPMENT(39,1)\|ENHANCED ROCK(38,1)\|LIQUID COLLECTION CONTAINER(35,10)\|SILICATE HUMIDITY(35,3)\|NATURAL RAINFALL(34,6)\|LINKAGE ROD(33,26)\|SALINE ALKALI SOIL(33,17)\|SALINE SOIL IMPROVEMENT(33,1)\|SEAT SUPPORT(32,17)\|SILICATE MINERAL(31,19)\|CIRCULATION AIR DUCT(31,5)\|CHEMICAL WEATHERING(28,18)\|NATURAL CONDITION(28,2)\|AIR CIRCULATION(24,15)\|CONTROLLABLE TEMPERATURE(24,3)\|HUMIDITY SENSOR(23,18)\|LEACHING SOLUTION(22,20)\|REFRIGERATOR(22,10)\|DRIVING PISTON(22,6)\|PUSH PULL ROD(21,17)\|MINERAL FERTILIZER(21,5)\|EXPERIMENTAL SUPPORT(20,4)\|LEACHING SOLUTION PUMPING(20,2)\|DEVIATION(20,1)\|THERMOSTAT(20,1)\|SILICATE TEMPERATURE(19,3)\|HUMIDITY ENVIRONMENT(19,2)\|LEACHING CHAMBER(19,2)\|SLIDING HOLE(18,6)\|SOIL TEMPERATURE(18,4)\|NATURAL PRECIPITATION CONDITION(18,2)\|LABORATORY(18,1)\|INFUSION TUBE(17,2)\|SILICATE MINERAL CHEMICAL WEATHERING(16,7)\|CONDITIONING AGENT(16,3)\|SPRAY BRACKET(16,3)\|HEAT PIPE(16,2)\|MESH PLATE(15,7)\|SILICATE RELATIVE HUMIDITY(14,3)\|LIQUID DELIVERY PIPE(14,2)\|SUPPORTING SPRAY(14,2)\|SYRINGE PUMP DRIVING(14,2)\|SOLENOID VALVE(14,1)\|LIQUID INLET(13,10)\|LIQUID OUTLET(13,10)\|LARGE DEVIATION(13,1)\|LIQUID ADDITION(13,1)\|SUPPORT FRAME(12,14)\|CIRCULATION DUCT(12,5)\|TEMPERATURE DETECTION(12,5)\|FILTER SCREEN(12,4)\|SYRINGE PUMP SUPPORT(12,3)\|LINK LEVER(11,9)\|CARBON FIXATION(11,4)\|NATURAL ENVIRONMENT(11,4)\|EQUAL LENGTH LINK ROD(11,3)\|DRIVING SHAFT(10,24)\|INJECTION PUMP(10,19)\|DRIVING LEVER(10,7)\|DRIVING MOTOR SHAFT(10,2)\|RAINFALL SIMULATOR(10,2)\|SUPPORT BASE(10,2)\|LEACHING COLUMN END(9,5)\|PRESET TEMPERATURE(9,5)\|SILICATE ROCK POWDER(9,2)\|EXPERIMENTAL SIMULATION AUTHENTICITY(9,1)\|LIQUID STORAGE CONTAINER(8,7)\|CHEMICAL WEATHERING SIMULATION EXPERIMENT(8,3)\|TIMING PULLEY(8,3)\|OPEN SHAPE(8,2)\|MULTIFUNCTIONAL SILICATE MINERAL CONDITIONER(8,1)\|DRIVING ROD(7,7)\|RELATIVE HUMIDITY(7,3)\|AIR RETURN OPENING(7,1)\|NUTRIENT SUPPLEMENTATION(7,1)\|REAL RAINFALL SIMULATION(7,1)\|SILICATE POWDER DISTURBANCE(7,1)\|GEAR(6,11)\|CARBON FIXING PROCESS DATA(6,3)\|SHOWER SOLUTION(6,3)\|SYNCHRONOUS BELT WHEEL(6,3)\|WATER INLET PIPE(6,3)\|DETECTING LEACHING LIQUID PRESSURE(6,2)\|HEATING AIR(6,2)\|NATURAL SALINE ALKALI SOIL(6,2)\|PRECIPITATION MINERAL CHEMICAL WEATHERING(6,2)\|RAINFALL SIMULATION DIAGRAM(6,2)\|RELIABLE WEATHERING REACTION(6,2)\|CONSTANT TEMPERATURE CAVITY INSIDE(6,1)\|LEACHING EXPERIMENT ACCURACY(6,1)\|RESEARCH SCIENTIFICITY(6,1)\|SALINE SOIL RECONSTRUCTION TREATMENT(6,1)\|SILICATE DISTURBANCE(6,1)\|SIMULATING LEACHING(6,1)\|PRESSURE SENSOR(5,7)\|AIR RETURN PIPE(5,4)\|INNER HOLE WALL(5,4)\|COLUMN ROCK MASS(5,2)\|TEMPERATURE REGULATION(5,2)\|TRANSFUSION TUBE(5,2)\|EXPERIMENTAL VERIFICATION(5,1)\|NOZZLE ATOMIZATION(5,1)\|OUTER CIRCUMFERENTIAL SURFACE(5,1)\|PAYING ATTENTION(5,1)\|PRECIPITATION SIMULATION(5,1)\|SALINE ALKALI SOIL HUMIDITY(5,1)\|SILICATE POWDER LEACHING SOLUTION(5,1)\|SUCKING LEACHING SOLUTION(5,1)\|TRANSPARENT OBSERVATION WINDOW(5,1)\|CONNECTING ROD(4,20)\|HEATING COMPONENT(4,5)\|CHEMICAL WEATHERING EXPERIMENT(4,2)\|HUMIDITY SENSOR FEED(4,2)\|INCUBATOR CONSTANT TEMPERATURE CAVITY(4,2)\|SPRAY COMPONENT(4,2)\|SPRAYING SUPPORT(4,2)\|SYRINGE DIRECTION(4,2)\|TRUE ACCURACY(4,2)\|1244 CIRCULATION FAN(4,1)\|ATOMIZING SPRAY HEAD(4,1)\|INCUBATOR HEATING(4,1)\|INSUFFICIENT NUTRIENT SUPPLY(4,1)\|LEACHING CAVITY(4,1)\|LEACHING SOLUTION CONCENTRATED IMPACT(4,1)\|LEACHING SOLUTION UNIFORMITY(4,1)\|PRESET HUMIDITY(4,1)\|CHAMBER DOOR(3,1)\|COLUMNAR ROCK TOP(3,1)\|CONSTANT TEMPERATURE INTRACAVITY REFRIGERATOR(3,1)\|HEAT PRESERVATION BOX(3,1)\|LEACHING COLUMN OPENING(3,1)\|MINERAL CONDITIONING AGENT DEVELOPMENT(3,1)\|MODIFIER(3,1)\|REAL SOIL CHANGE(3,1)\|	(CN121454002)\|1. An leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, comprising:\| The temperature control device comprises a support frame and an incubator device arranged on the support frame; \| The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; \| a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; \| a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and \|And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.\|2. The leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions according to claim 1, wherein the rainfall simulation device comprises a spraying assembly arranged at an opening at the top end of the leaching column, a syringe pump mechanism for drawing and pumping leaching solution, a liquid delivery pipe for connecting the spraying assembly and a liquid outlet port of the syringe pump mechanism, a water inlet pipe for connecting a liquid inlet port of the syringe pump mechanism with a liquid storage container, and a supporting seat for supporting the syringe pump mechanism, the syringe pump mechanism is fixedly arranged on the supporting seat, the leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions further comprises a driving device for driving the syringe pump mechanism to draw and pump leaching solution, a first valve arranged at the liquid inlet port of the syringe pump mechanism and a second valve arranged at the liquid outlet port of the syringe pump mechanism, the driving device is arranged on the supporting seat, and the controller can control the driving device, the first valve and the second valve to work, and the driving device and the second valve are respectively electrically connected with the controller.\|3. The leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 2, wherein the injection pump mechanism comprises an injection cylinder with two open ends, a first piston arranged in the injection cylinder in a sliding manner, a second piston arranged in the injection cylinder in a sliding manner, a push-pull rod for driving the first piston to move along the axial direction of the injection cylinder, a first linkage rod connected with one end of the push-pull rod far away from the first piston, a sleeve for driving the second piston to move along the axial direction of the injection cylinder, and a second linkage rod connected with one end of the sleeve far away from the second piston, wherein a first sliding hole for the push-pull rod to pass through is arranged on the second piston, the outer circumferential surface of the push-pull rod is in interference contact with the inner hole wall of the first sliding hole, the sleeve is sleeved on the rod in an axial sliding manner, and the first linkage rod and the second linkage rod are respectively connected with the driving device.\|4. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 3, wherein the driving means comprises a driving assembly, a link mechanism connecting the first link rod with the second link rod, and a gear mechanism connecting the link mechanism with the driving assembly, the gear mechanism comprising a first gear rotatably mounted on the support base and a second gear rotatably mounted on the support base, the first gear and the second gear being engaged, the first gear and/or the second gear being connected with the driving assembly so that the driving assembly can drive the first gear and the second gear to rotate synchronously, the link mechanism comprising a first link rod fixedly connected with the first gear, a first link rod rotatably connecting a first end of the first link rod with a first end of the first link rod, a second gear rotatably connecting a second end of the first link rod with a second end of the first link rod, a second gear fixedly connected with a second end of the second link rod, a second link rod of equal length, a second link rod rotatably connecting a second end of the second link rod with a second end of the second link rod, a second link rod of equal length, and a second link rod of equal length.\|5. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions of claim 4, wherein the driving assembly comprises a first driving shaft rotatably disposed on the supporting seat, a second driving shaft rotatably disposed on the supporting seat, a driving motor fixedly mounted on the supporting seat, a first synchronous pulley fixedly sleeved on the first driving shaft, a second synchronous pulley fixedly sleeved on the second driving shaft, a third synchronous pulley fixedly sleeved on a motor shaft of the driving motor, and a synchronous belt connecting the first synchronous pulley, the second synchronous pulley and the third synchronous pulley, wherein the driving motor is electrically connected with the controller.\|6. A leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 3, wherein a pressure sensor for detecting leaching liquid pressure in the injection cylinder is arranged in the injection cylinder, and the pressure sensor is electrically connected with the controller.\|7. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions of claim 1, wherein the leaching assembly further comprises a first mesh plate disposed in a leaching chamber within the leaching column and a first filter screen laid on the mesh plate, the silicate rock powder in the leaching column forming a columnar rock mass, a bottom end of the columnar rock mass being supported on the first mesh plate.\|8. The leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 1, wherein the incubator device comprises an incubator with a constant temperature cavity inside, a refrigerator arranged on the incubator to selectively open or close the constant temperature cavity, a refrigerator arranged inside the incubator to realize temperature regulation in the constant temperature cavity, and an air circulation and heating mechanism arranged inside the incubator, wherein the air circulation and heating mechanism can accelerate air circulation flow in the constant temperature cavity and heat air in the constant temperature cavity, the controller can control the refrigerator and the air circulation and heating mechanism to work according to humidity and temperature detected by the temperature and humidity sensor, and the temperature in the constant temperature cavity is regulated so as to keep the temperature in the constant temperature cavity within a preset temperature range of 0-25 ℃.\|9. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 8, wherein the air circulation and heat supply mechanism comprises a circulation air duct arranged in the constant temperature cavity, an air inlet pipe communicated with an air inlet of the circulation air duct, an air return pipe communicated with an air return opening of the circulation air duct, a heating assembly arranged in the circulation air duct, and a circulation fan arranged in the circulation air duct, and the heating assembly comprises a plurality of heating pipes which are transversely arranged.\|10. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to any one of claims 2 to 6, wherein the spray assembly comprises a spray head connected to the infusion tube and a spray bracket for supporting the spray head on the support frame and/or at the top end of the leaching column, the spray bracket being detachably connected to the support frame and/or the leaching column.	(CN121454002)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction treatment, and particularly relates to leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions.\|BACKGROUND ART\|[0002] The saline-alkali soil has the problems of deterioration of physical and chemical properties of soil, insufficient nutrient supply, limited plant growth and the like due to high salt content and strong alkalinity.\|[0003] The conventional saline-alkali soil improvement methods comprise salt removal, salt pressing, organic fertilizer application, chemical modifier application and the like, but the methods have the defects of slow effect, high cost, high environmental risk or difficult long-term maintenance of improvement effect and the like. In recent years, mineral fertilizers have been greatly developed in the aspect of saline-alkali soil improvement, silicate minerals are utilized for weathering to release nutrient elements such as calcium, magnesium, potassium, phosphorus and the like, carbonate minerals are formed by reaction with atmospheric carbon dioxide, and research on soil improvement, nutrient supplementation, carbon fixation and sink increase is increasingly paid attention to. However, the existing research is still imperfect in simulating leaching and chemical weathering rules of silicate minerals under the conditions of natural precipitation and soil temperature and humidity, and lacks experimental verification and model support of a system. In practical researches, the following problems are common in the conventional silicate mineral chemical weathering leaching experimental device:\| (1) By adopting a manual liquid adding mode, the leaching solution amount is difficult to be matched with the natural precipitation condition; \| (2) Only is carried out at room temperature, lacks heating and temperature control functions, and cannot reflect the change of the real soil under the temperature and humidity conditions. \|[0004] The problems cause great deviation between laboratory simulated silicate mineral weathering experimental results and chemical weathering under actual natural conditions, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain. Therefore, development of a chemical weathering leaching experimental device capable of simulating silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment is needed to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners and novel mineral fertilizers.\|DISCLOSURE\|Disclosure of Invention\|[0005] Based on the problem that the laboratory simulation silicate mineral weathering experimental result in the prior art has larger deviation from the chemical weathering under the actual natural condition, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain, the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions, which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable temperature and humidity conditions, so as to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and provide scientific basis and experimental support for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers.\|[0006] In order to achieve the purpose, the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided, and comprises:\| The temperature control device comprises a support frame and an incubator device arranged on the support frame; \| The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; \| a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; \| a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and \|And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.\|[0007] Further, the rainfall simulation device comprises a spraying component arranged at the open top of the leaching column, a syringe pump mechanism for drawing and pumping leaching solution, a liquid delivery pipe for connecting the spraying component with a liquid outlet port of the syringe pump mechanism, a water inlet pipe for connecting a liquid inlet port of the syringe pump mechanism with a liquid storage container, and a supporting seat for supporting the syringe pump mechanism, wherein the syringe pump mechanism is fixedly arranged on the supporting seat, the leaching device for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity further comprises a driving device for driving the syringe pump mechanism to draw and pump leaching solution, a first valve arranged at the liquid inlet port of the syringe pump mechanism and a second valve arranged at the liquid outlet port of the syringe pump mechanism, the driving device is arranged on the supporting seat, and the driving device, the first valve and the second valve can be controlled to work and are respectively and electrically connected with the controller.\|[0008] Further, the injection pump mechanism comprises an injection cylinder, a first piston, a second piston, a push-pull rod, a first linkage rod, a sleeve and a second linkage rod, wherein the two ends of the injection cylinder are respectively in an opening shape, the first piston is arranged in the injection cylinder in a sliding mode, the second piston is arranged in the injection cylinder in a sliding mode, the push-pull rod is used for driving the first piston to move along the axial direction of the injection cylinder, the first linkage rod is connected with one end, far away from the first piston, of the push-pull rod, the sleeve is used for driving the second piston to move along the axial direction of the injection cylinder, the second linkage rod is connected with one end, far away from the second piston, of the sleeve, a first sliding hole is formed in the second piston, the outer peripheral surface of the push-pull rod is in interference contact with the inner hole wall of the first sliding hole, the sleeve can be sleeved on the push-pull rod in an axial sliding mode, and the first linkage rod and the second linkage rod are respectively connected with the driving device.\|[0009] Further, the driving device comprises a driving assembly, a connecting rod mechanism connecting the first linkage rod with the second linkage rod, and a gear mechanism connecting the connecting rod mechanism with the driving assembly, wherein the gear mechanism comprises a first gear rotatably installed on the supporting seat and a second gear rotatably installed on the supporting seat, the first gear is meshed with the second gear, the first gear and/or the second gear are/is connected with the driving assembly so that the driving assembly can drive the first gear and the second gear to synchronously rotate, the connecting rod mechanism comprises a first driving rod fixedly connected with the first gear, a first connecting rod rotatably connecting the first end of the first driving rod with the first end of the first linkage rod, a second connecting rod rotatably connecting the second end of the first driving rod with the first end of the second linkage rod, a second driving rod fixedly connected with the second gear, a second connecting rod fixedly connected with the second end of the second driving rod, a second connecting rod fixedly connected with the second end of the second connecting rod, a second connecting rod with the second connecting rod, and a first connecting rod with the second connecting rod, and a second connecting rod with the second connecting rod, and the connecting rod with the second connecting rod with the first connecting rod and the second connecting rod with the second connecting rod.\|[0010] Further, the driving assembly comprises a first driving shaft arranged on the supporting seat in a rotating mode, a second driving shaft arranged on the supporting seat in a rotating mode, a driving motor fixedly installed on the supporting seat, a first synchronous belt wheel fixedly sleeved on the first driving shaft, a second synchronous belt wheel fixedly sleeved on the second driving shaft, a third synchronous belt wheel fixedly sleeved on a motor shaft of the driving motor, and a synchronous belt connecting the first synchronous belt wheel, the second synchronous belt wheel and the third synchronous belt wheel, wherein the driving motor is electrically connected with the controller.\|[0011] Further, a pressure sensor for detecting the leaching solution pressure in the injection cylinder is arranged in the injection cylinder, and the pressure sensor is electrically connected with the controller.\|[0012] Further, the leaching assembly further comprises a first mesh plate arranged in a leaching cavity in the leaching column and a first filter screen paved on the mesh plate, silicate rock powder in the leaching column forms a columnar rock body, and the bottom end of the columnar rock body is supported on the first mesh plate.\|[0013] Further, the incubator device includes the incubator that inside was equipped with the constant temperature chamber, set up in on the incubator in order to open or close selectively the chamber door in constant temperature chamber, set up in inside in order to realize the refrigerator of constant temperature intracavity temperature regulation of incubator, and set up in inside air cycle and the heating mechanism of incubator, air cycle and the heating mechanism can be accelerated air cycle flow in the constant temperature chamber, and heat air in the constant temperature chamber, the controller can be according to humidity and the temperature control that temperature and humidity sensor detected the refrigerator air cycle and the heating mechanism work, adjust the temperature in the constant temperature chamber, so that the temperature in the constant temperature chamber keeps in the preset temperature range of 0 ℃ to 25 ℃.\|[0014] Further, the air circulation and heat supply mechanism comprises a circulation air channel arranged in the constant temperature cavity, an air inlet pipe communicated with an air inlet of the circulation air channel, an air return pipe communicated with an air return port of the circulation air channel, a heating component arranged in the circulation air channel and a circulation fan arranged in the circulation air channel, wherein the heating component comprises a plurality of heating pipes which are transversely arranged.\|[0015] Further, the spraying assembly comprises a spray head connected with the infusion tube and a spraying support for supporting the spray head on the support frame and/or at the top end of the leaching column, and the spraying support is detachably connected with the support frame and/or the leaching column.\|[0016] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:\| According to the leaching equipment for simulating chemical weathering under the natural temperature and humidity conditions of silicate rock powder, which is disclosed by the embodiment of the invention, the actual natural rainfall and the natural saline-alkali soil temperature and humidity conditions can be simulated, and mineral chemical weathering of the precipitation amount is simulated according to the actual temperature and humidity of the saline-alkali soil, so that the chemical weathering process of silicate minerals in the natural environment of the saline-alkali soil is simulated truly, the true accuracy of the silicate mineral chemical weathering experimental result is improved, and the reliable weathering reaction, salt replacement and carbon fixing process data of the silicate minerals in the saline-alkali soil are obtained, so that scientific basis and experimental support are provided for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers. \|DRAWINGS DESCRIPTION\|[0017] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0018] FIG. 1 is a schematic diagram of a three-dimensional structure of leaching equipment simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions;\| FIG. 2 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 3 is a schematic top view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 4 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 5 is an assembly diagram of a rainfall simulation device and a driving device according to an embodiment of the present invention in a first working state; \| FIG. 6 is a schematic cross-sectional view of the structure shown in FIG. 5; \| fig. 7 is an assembly diagram of the rainfall simulation device and the driving device provided by the embodiment of the invention in a second working state; \| FIG. 8 is a schematic top view of the structure shown in FIG. 7; \| FIG. 9 is a schematic cross-sectional view of the structure shown in FIG. 7; \| Fig. 10 is a schematic perspective view of a leaching assembly according to an embodiment of the present invention; \| FIG. 11 is a schematic cross-sectional view of a leaching assembly according to an embodiment of the present invention; \| FIG. 12 is an exploded view of a leaching assembly provided by an embodiment of the present invention; \| FIG. 13 is a schematic perspective view of an incubator assembly according to an embodiment of the present invention; \| Fig. 14 is a schematic cross-sectional structure of an incubator assembly according to an embodiment of the present invention. \|[0019] Wherein, each reference sign in the figure:\| 1-temperature control device, 11-supporting frame, 12-incubator device, 121-incubator, 122-oven door, 123-refrigerator, 124-air circulation and heat supply mechanism, 1241-circulation air duct, 1242-muffler, 1243-heating assembly, 1244-circulation fan, 1245-air inlet pipe, 125-mounting hole and 126-observation window; \| 2-leaching components, 21-leaching columns, 22-liquid collecting containers, 23-liquid discharge pipes, 24-first mesh plates, 25-first filter screens, 26-second filter screens and 27-second mesh plates; \| 3-a rainfall simulation device, 31-a spray assembly, 311-a spray head, 312-a spray bracket, 32-a syringe pump mechanism, 321-a syringe, 322-a first piston, 323-a second piston, 324-a push-pull rod, 325-a first linkage rod, 326-a sleeve, 327-a second linkage rod, 33-a transfusion tube, 34-a water inlet tube and 35-a supporting seat; \| 4-drive means, 41-drive assembly, 411-first drive shaft, 412-second drive shaft, 413-drive motor, 414-first timing pulley, 415-second timing pulley, 416-third timing pulley, 417-timing belt, 418-motor shaft, 42-link mechanism, 421-first drive rod, 422-first link, 423-second link, 424-second drive rod, 425-third link, 426-fourth link, 43-gear mechanism, 431-first gear, 432-second gear; \| 5-fixed support, 6-bolt piece, 7-liquid storage space, 8-columnar rock mass and 9-controller. \|INVENTION MODE\|Detailed Description\|[0020] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0021] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, features defining "first," "second," and "third" may explicitly or implicitly include one or more such features. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0022] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.\|[0023] Referring to fig. 1 to 14, a description will now be given of an leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention. Referring to fig. 1, fig. 2, fig. 3 and fig. 4 in combination, the leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions provided by the embodiment of the invention comprises a temperature control device 1, a leaching assembly 2, a rainfall simulation device 3, a temperature and humidity sensor and a controller 9, wherein the temperature control device 1 comprises a support frame 11 and a constant temperature box device 12 arranged on the support frame 11. The leaching assembly 2 comprises a leaching column 21 arranged in the incubator device 12 and a liquid collecting container 22 arranged below the leaching column 21, wherein two axial ends of the leaching column 21 respectively extend out of the incubator device 12, the top end of the leaching column 21 is open, and a liquid discharging pipe 23 communicated with the liquid collecting container 22 is arranged at the bottom end of the leaching column 21. Wherein, the leaching column 21 is a column-shaped leaching container made of high-temperature resistant transparent plastic or high-temperature resistant transparent organic glass. The rainfall simulation device 3 is used for simulating rainfall so that the leaching solution can uniformly flow into silicate rock powder in the leaching column 21 through the top end opening of the leaching column 21. The temperature and humidity sensor is used for detecting the temperature and humidity of silicate rock powder in the leaching column 21 in real time, and a probe of the temperature and humidity sensor is inserted into the leaching column 21. It should be noted that, the temperature and humidity sensor is implemented by adopting the prior art, and its working principle and structure are well known to those skilled in the art, and are not described herein. The controller 9 is used for controlling the rainfall simulation device 3 and the incubator device 12 to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of the silicate rock powder in the leaching column 21 is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column 21 is maintained at 30-80%. It should be noted that the controller 9 may be, but is not limited to, a programmable logic controller.\|[0024] The basic working principle of the leaching equipment for simulating chemical weathering of silicate rock powder under the natural temperature and humidity condition is that silicate rock is crushed into silicate rock powder with the particle size of 0.1 micron, the silicate rock powder and a certain amount of saline-alkali soil are uniformly mixed and filled in a leaching column 21 of a leaching assembly 2, and a rainfall simulation device 3 is arranged at the opening at the top end of the leaching column 21. The simulated rainfall device 3 carries out real simulated rainfall characteristics on the leaching solution, so that the leaching solution can flow into the silicate rock powder in the leaching column 21 through the opening at the top end of the leaching column 21, the silicate rock powder in the leaching column 21 can be uniformly leached, disturbance on the silicate rock powder in the leaching column 21 is reduced, leaching efficiency and leaching effect of the silicate rock powder in the leaching column 21 are improved, and accuracy of silicate mineral chemical weathering experimental results is improved. In addition, during leaching, the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, and after the leaching solution permeates the silicate rock powder in the leaching column 21, the leaching solution is drained into the liquid collecting container 22 through the liquid drain pipe 23 at the bottom end of the leaching column 21. And, in the whole process of the chemical weathering experiment, the temperature in the incubator device 1 and the humidity in the leaching column 21 are detected in real time through the temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is less than 0 ℃, the controller 9 controls the heating component in the incubator device 1 to heat and work until the temperature in the incubator device 1 reaches 25 ℃, and the controller 9 controls the heating component in the incubator device 1 to stop heating and work. When the temperature in the oven apparatus 1 is greater than 25 ℃, the controller 9 controls the refrigerator in the oven apparatus 1 to operate until the temperature in the oven apparatus 1 reaches 25 ℃, and the controller 9 controls the refrigerator in the oven apparatus 1 to stop the cooling operation. The circulation is such that the temperature in the oven apparatus 1 is controlled within a preset temperature range of 0 to 25 ℃, thereby making the silicate rock powder in the leaching column 21 subjected to the chemical weathering simulation experiment under the temperature condition of 0 to 25 ℃. Of course, the controller 9 may also control the operation of the heating element and/or the refrigerator in the incubator apparatus 1 so that the temperature in the incubator apparatus 1 is stabilized at any one of the preset temperature values between 0 ℃ and 25 ℃ and so that the silicate powder in the leaching column 21 is subjected to chemical weathering simulation test under a specific temperature condition (e.g., 5 ℃, 10 ℃, 15 ℃, 20 ℃,25 ℃ or the like) between 0 ℃ and 25 ℃. Meanwhile, when the humidity in the leaching column 21 is less than 30%, the controller 9 controls the rainfall simulation device 3 to work, so that the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, until the humidity in the leaching column 21 reaches 80%, the controller 9 controls the rainfall simulation device 3 to stop working, and the circulation is performed in such a way that the humidity in the leaching column 21 is controlled within a preset humidity range of 30-80%, and thus chemical weathering simulation experiments are performed on the silicate rock powder in the leaching column 21 under a humidity condition of 30-80%. Therefore, the method can simulate the actual natural rainfall and the natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, simulate the mineral chemical weathering of the precipitation according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and improve the true accuracy of the silicate mineral chemical weathering experimental result so as to obtain the reliable weathering reaction, salt replacement and carbon fixation process data of the silicate minerals of the saline-alkali soil, thereby being beneficial to improving the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|[0025] Referring to fig. 2,3 and 4, in some embodiments, the rainfall simulation device 3 includes a spray assembly 31 disposed at an opening at a top end of the leaching column 21, a syringe pump mechanism 32 for drawing and pumping the leaching solution, a transfusion tube 33 connecting the spray assembly 31 and a liquid outlet port of the syringe pump mechanism 32, a water inlet pipe 34 for connecting a liquid inlet port of the syringe pump mechanism 32 with a liquid storage container, and a support seat 35 for supporting the syringe pump mechanism 32, the syringe pump mechanism 32 is fixedly mounted on the support seat 35, the leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions further includes a driving device 4 for driving the syringe pump mechanism 32 to draw and pump the leaching solution, a first valve disposed at the liquid inlet port of the syringe pump mechanism 32 and a second valve disposed at the liquid outlet port of the syringe pump mechanism 32, the driving device 4 is disposed on the support seat 35, and the controller 9 can control the driving device 4, the first valve and the second valve to work, and the driving device 4, the first valve and the second valve are respectively electrically connected with the controller 9. It will be appreciated that in some of these embodiments the first valve 9 and the second valve 10 are solenoid valves. By the above arrangement, the silicate rock is crushed into silicate rock powder having a particle size of 0.1 μm, the silicate rock powder is packed in the leaching column 21 of the leaching assembly 2, and the spraying assembly 31 is installed at the top end opening of the leaching column 21. When the injection pump mechanism 32 is required to be used for sucking the leaching solution from the liquid storage container under the negative pressure, the controller controls the first valve 9 to open the liquid inlet of the injection pump mechanism 32, the controller controls the second valve 10 to close the liquid outlet of the injection pump mechanism 32, the driving device 4 drives the injection pump mechanism 32 to suck the leaching solution from the liquid storage container under the negative pressure, until the leaching solution in the injection pump mechanism 32 is full, the controller controls the first valve 9 to close the liquid inlet of the injection pump mechanism 32, and the controller controls the second valve 10 to open the liquid outlet of the injection pump mechanism 32, the injection pump mechanism 32 can pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the simulated rainfall device 3 under the driving action of the driving device 4, the real rainfall simulation characteristic is realized, the uniformity of the silicate powder in the leaching column 21 is ensured, the silicate powder in the leaching column 21 is uniformly leached, the disturbance of the silicate powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate powder in the leaching column 21 are further improved, and the accuracy of silicate mineral chemical weathering experiment results is facilitated. In addition, during leaching, the leaching solution of the silicate powder in the leaching column 21 is uniformly sprayed to the leaching column 21 at a certain flow rate through the spraying assembly 31, and is drained into the liquid collecting container 22 through the drain pipe 23 at the bottom end of the leaching column 21 after penetrating the silicate powder in the leaching column 21.\|[0026] Therefore, in the leaching device for simulating chemical weathering of silicate rock powder under the natural temperature and humidity conditions, when the controller controls the first valve 9 to be opened and the second valve 10 to be closed, the driving device 4 can drive the injection pump mechanism 32 to draw the leaching solution from the liquid storage container through negative pressure until the injection pump mechanism 32 draws enough leaching solution, then the controller controls the first valve 9 to be closed and the second valve 10 to be opened, the injection pump mechanism 32 can continuously pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the rainfall simulator 3 under the driving action of the driving device 4, the real rainfall simulation characteristic of the spraying assembly 31 of the rainfall simulator 3 is adopted to ensure the uniformity of the leaching solution flowing into the silicate rock powder in the leaching column 21, so that the silicate rock powder in the leaching column 21 can be uniformly leached, the disturbance of the silicate rock powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate rock powder in the leaching column 21 are improved, and the accuracy of the silicate mineral chemical weathering experiment result is improved.\|[0027] Referring to fig. 2,6 and 9 in combination, in some embodiments, the syringe pump mechanism 32 includes a syringe 321, a first piston 322, a second piston 323, a push-pull rod 324, a first linkage rod 325, a sleeve 326 and a second linkage rod 327, two ends of the syringe 321 are all open, the first piston 322 and the second piston 323 are respectively slidably disposed in the syringe 321, and when the first piston 322 and the second piston 323 are respectively slid to the openings at two ends of the syringe 321, a closed liquid storage space 7 for storing the shower solution can be formed in the syringe 321, and the liquid storage capacity of the liquid storage space 7 can be preset. The push-pull rod 324 is used for driving the first piston 322 to move along the axial direction of the injection cylinder 321, the sleeve 326 is used for driving the second piston 323 to move along the axial direction of the injection cylinder 321, and when the first piston 322 and the second piston 323 move away from each other along the axial direction of the injection cylinder 321, the solution can be pumped from the liquid storage container through the injection pump mechanism 32, and the pumped solution can be stored in the closed liquid storage space 7 between the first piston 322 and the second piston 323. When the first piston 322 and the second piston 323 move closer to each other in the axial direction of the syringe 321, the shower solution in the solution storage space 7 can be continuously pumped to the shower assembly 31 of the rainfall simulation device 3 by the syringe pump mechanism 32. The first linkage rod 325 is connected with one end of the push-pull rod 324 far away from the first piston 322, the second linkage rod 327 is connected with one end of the sleeve 326 far away from the second piston 323, the first linkage rod 325 and the second linkage rod 327 are respectively connected with the driving device 4, a first sliding hole for the push-pull rod 324 to pass through is arranged on the second piston 323, the outer peripheral surface of the push-pull rod 324 is in interference contact with the inner hole wall of the first sliding hole, and the sleeve 326 can be sleeved on the push-pull rod 324 in an axial sliding manner. When the driving device 4 drives the first linkage rod 325 and the second linkage rod 327, the sleeve 326 is sleeved on the push-pull rod 324 in a sliding manner along the axial direction, so that the first piston 322 and the second piston 323 can move towards or away from each other along the axial direction of the injection cylinder 321. It should be noted that, the liquid inlet port and the liquid outlet port are both disposed on the syringe 321, and the liquid inlet port and the liquid outlet port are respectively communicated with the liquid storage space 7.\|[0028] Referring to fig. 4, 5, 7 and 8 in combination, in some embodiments, the driving device 4 includes a driving assembly 41, a link mechanism 42 and a gear mechanism 43, the link mechanism 42 is used to connect the first link lever 325 with the second link lever 327, the gear mechanism 43 is used to connect the link mechanism 42 with the driving assembly 41, the gear mechanism 43 includes a first gear 431 rotatably mounted on the support seat 35 and a second gear 432 rotatably mounted on the support seat 35, the first gear 431 and the second gear 432 are the same in size and structure, the first gear 431 and the second gear 432 mesh, the first gear 431 and the second gear 432 are connected with the driving assembly 41, and one gear of the first gear 431 and the second gear 432 may be connected with the driving assembly 41, so that the driving assembly 41 can drive the first gear 431 and the second gear 432 to rotate synchronously. The link mechanism 42 includes a first driving lever 421 fixedly coupled to a first gear 431, a first link 422 rotatably coupling a first end of the first driving lever 421 with a first end of a first link lever 325, a second link 423 rotatably coupling a second end of the first driving lever 421 with a first end of a second link lever 327, a second driving lever 424 fixedly coupled to a second gear 432, a third link 425 rotatably coupling a first end of the second driving lever 424 with a second end of the first link lever 325, a fourth link 426 rotatably coupling a second end of the second driving lever 424 with a first end of the second link lever 327, the lengths of the first link 422, the second link 423, the third link 425, and the fourth link 426 being equal, the length of the first link lever 325 being equal to the length of the second link lever 327, and the length of the first driving lever 421 being equal to the length of the second link lever 424. It should be noted that, two ends of the first link 422 are respectively rotatably connected to the first end of the first driving rod 421 and the first end of the first linkage rod 325 through a pivot, and two ends of the second link 423 are respectively rotatably connected to the second end of the first driving rod 421 and the second end of the first linkage rod 325 through a pivot. Through the above structure, the driving assembly 41 can synchronously drive the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321, and can improve the stability of the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321. In addition, the connecting rod mechanism 42 is driven by the rotation of the gear mechanism 43 to drive the first piston 322 and the second piston 323 to move close to each other along the axial direction of the injection cylinder 321, and the speed of the injection pump mechanism 32 for pumping the leaching solution can be controlled by controlling the rotation speed of the first gear 431 and/or the second gear 432, so that the leaching rate can be controlled and regulated according to the leaching experiment requirement.\|[0029] Referring to fig. 4, 5 and 7, in some embodiments, the driving assembly 41 includes a first driving shaft 411, a second driving shaft 412, a driving motor 413, a first synchronous belt 417 wheel 414, a second synchronous belt 417 wheel 415, a third synchronous belt 417 wheel 416 and a synchronous belt 417, the first driving shaft 411 and the second driving shaft 412 are respectively rotatably disposed on the supporting seat 35, the driving motor 413 is fixedly mounted on the supporting seat 35, the first synchronous belt 417 wheel 414 is fixedly sleeved on the first driving shaft 411, the second synchronous belt 417 wheel 415 is fixedly sleeved on the second driving shaft 412, the third synchronous belt 417 wheel 416 is fixedly sleeved on a motor shaft 418 of the driving motor 413, and the synchronous belt 417 connects the first synchronous belt 417 wheel 414, the second synchronous belt 417 wheel 415 and the third synchronous belt 417 wheel 416, and the driving motor 413 is electrically connected with the controller. Through the above structure arrangement, under the driving action of the driving motor 413, the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 synchronously rotate, so as to drive the gear mechanism 43 to rotate, and the gear mechanism 43 drives the first piston 322 and the second piston 323 to move close to or far away from each other along the axial direction of the injection cylinder 321 through the link mechanism 42, so that the injection pump mechanism 32 can finish the action of drawing and pumping the shower solution.\|[0030] Referring to fig. 2, 4 and 5, in some embodiments, the first gear 431 is fixedly sleeved on the first driving shaft 411, the second gear 432 is fixedly sleeved on the second driving shaft 412, and the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are arranged in an isosceles triangle, so that the distance between the first driving shaft 411 and the second driving shaft 412, the distance between the first driving shaft 411 and the motor shaft 418 of the driving motor 413, and the distance between the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are all equal. By the above arrangement, the stability of the movement of the first piston 322 and the second piston 323 in the axial direction of the syringe 321 toward each other or away from each other can be improved.\|[0031] In some embodiments, a pressure sensor for detecting leaching liquid pressure inside the syringe 321 is disposed in the syringe 321, and the pressure sensor is electrically connected to the controller. The controller can control the rotation speed of the driving motor 413 to control the rotation speed of the first gear 431 and/or the second gear 432 according to the pressure detected by the pressure sensor, so as to control the speed of the injection pump mechanism 32 for pumping the leaching solution, thereby being convenient for controlling and adjusting the leaching rate according to the leaching experiment requirement.\|[0032] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a first mesh plate 24 disposed in the leaching chamber in the leaching column 21 and a first filter screen 25 laid on the mesh plate, silicate rock powder in the leaching column 21 forms a columnar rock body 8, and a bottom end of the columnar rock body 8 is supported on the first mesh plate 24. Through the structure setting, through adopting the first mesh board 24 that plastics or metal etc. made to the silicate rock powder in the leaching column 21 to form column rock mass 8 bottom formation support, the leaching solution after the rethread first filter screen 25 on the first mesh board 24 filters, can prevent effectively that the silicate rock powder in the leaching column 21 from forming column rock mass 8 bottom and collapsing, ensure simultaneously that the leaching solution that liquid collecting container 22 collected does not contain silicate rock powder, be favorable to improving the accuracy of leaching experiment. The mesh size of the first screen 25 is smaller than the particle size of the silicate powder.\|[0033] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a second screen 26 disposed on top of the columnar rock mass 8 and a second mesh plate 27 disposed over the second screen 26. By paving the second filter screen 26 on the top end of the columnar rock body 8 formed by silicate rock powder in the leaching column 21 and covering the second filter screen 26 with a second mesh plate 27 made of hard materials such as plastics or metals, the integrity of the top of the columnar rock body 8 is prevented from being damaged due to the fact that the concentrated impact of leaching solution water flows form a dent.\|[0034] Referring to fig. 2 and 4 in combination, in some embodiments, spray assembly 31 includes a spray head 311 coupled to a fluid line 33, and a spray bracket 312 for supporting spray head 311 on support frame 1 and/or on the top of leaching column 21, spray bracket 312 being removably coupled to support frame 1 and/or leaching column 21. It should be noted that the spray head 311 may be, but is not limited to, an atomizing spray head 311. In actual operation, the speed of the driving motor 413 is controlled, and various rainfall is simulated by adopting the atomizing nozzle 311, so that silicate rock powder in the leaching column 21 forms a columnar rock body 8, and the problems that the soil column structure is damaged and the leaching speed of water is influenced due to the fact that water flow impacts to form a recess are avoided.\|[0035] Referring to fig. 13 and 14 in combination, in some embodiments, the incubator apparatus 12 includes an incubator 121 having a constant temperature chamber therein, a door 122 provided on the incubator 121 to selectively open or close the constant temperature chamber, a refrigerator 123 provided inside the incubator 121 to achieve temperature adjustment in the constant temperature chamber, and an air circulation and heat supply mechanism 124 provided inside the incubator 121, the air circulation and heat supply mechanism 124 being capable of accelerating the air circulation flow in the constant temperature chamber and heating the air in the constant temperature chamber, and the controller 9 being capable of controlling the operation of the refrigerator 123, the air circulation and heat supply mechanism 124 according to the humidity and temperature detected by the temperature and humidity sensor to adjust the temperature in the constant temperature chamber so as to maintain the temperature in the constant temperature chamber within a preset temperature range of 0 to 25 ℃ or to any specific temperature value between 0 to 25 ℃. The incubator 121 is provided with a mounting hole 125 for accommodating and mounting the leaching column 21, and the outer side wall of the leaching column 21 is in airtight contact with the inner hole wall of the mounting hole 125. The door 122 is provided with a transparent observation window 126 made of high temperature resistant glass so as to observe leaching conditions in the leaching column 21 inside the incubator 121. In the whole process of chemical weathering experiment, the temperature in the incubator device 1 is detected in real time through a temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is smaller than 0 ℃, the controller 9 controls the refrigerator 123 to be closed and controls the air circulation and heat supply mechanism 124 in the heat preservation 121 to work, and the air circulation and heat supply mechanism 124 accelerates the air circulation flow in the constant temperature cavity and heats the air in the constant temperature cavity, so that the temperature in the constant temperature cavity of the incubator 121 is quickly increased until the temperature in the constant temperature cavity of the incubator 121 reaches 25 ℃, and the controller 9 controls the air circulation and heat supply mechanism 124 in the incubator device 1 to stop heating work. If the temperature in the constant temperature chamber of the incubator 121 is higher than 25 ℃, the controller 9 controls the refrigerator 123 to operate and controls the air circulation and heating mechanism 124 to stop operating, so that the temperature in the constant temperature chamber is reduced by between 0 and 25 ℃. By means of the circulation, the temperature in the heat preservation box 121 can be controlled within a preset temperature range of 0-25 ℃, so that silicate rock powder in the leaching column 21 is subjected to chemical weathering simulation experiments under the temperature condition of 0-25 ℃ to simulate actual natural rainfall and natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, mineral chemical weathering of simulated precipitation is performed according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and the actual accuracy of silicate mineral chemical weathering experiment results is improved.\|[0036] Referring to fig. 13 and 14 in combination, in some embodiments, the air circulation and heat supply mechanism 124 includes a circulation duct 1241 disposed in the constant temperature chamber, an air inlet pipe 1245 connected to an air inlet of the circulation duct 1241, an air return pipe 1242 connected to an air return port of the circulation duct 1241, a heating assembly 1243 disposed in the circulation duct 1241, and a circulation fan 1244 disposed in the circulation duct 1241, the heating assembly 1243 including a plurality of heating pipes disposed transversely. When the air circulation and heat supply mechanism 124 works, air in the constant temperature cavity is led into the circulation air channel 1241 by the air inlet pipe 1245 under the action of the circulation fan 45, the air in the circulation air channel 1241 is heated by the heating component 1244 and then becomes hot air, and the hot air in the circulation air channel 1241 flows back to the constant temperature cavity by the air return pipe 1243, so that the air circulation and heat supply mechanism 124 can be used for quickly heating the air in the constant temperature cavity.\|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.	(CN121454002)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction treatment, and particularly relates to leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions.\|BACKGROUND ART\|[0002] The saline-alkali soil has the problems of deterioration of physical and chemical properties of soil, insufficient nutrient supply, limited plant growth and the like due to high salt content and strong alkalinity.\|[0003] The conventional saline-alkali soil improvement methods comprise salt removal, salt pressing, organic fertilizer application, chemical modifier application and the like, but the methods have the defects of slow effect, high cost, high environmental risk or difficult long-term maintenance of improvement effect and the like. In recent years, mineral fertilizers have been greatly developed in the aspect of saline-alkali soil improvement, silicate minerals are utilized for weathering to release nutrient elements such as calcium, magnesium, potassium, phosphorus and the like, carbonate minerals are formed by reaction with atmospheric carbon dioxide, and research on soil improvement, nutrient supplementation, carbon fixation and sink increase is increasingly paid attention to. However, the existing research is still imperfect in simulating leaching and chemical weathering rules of silicate minerals under the conditions of natural precipitation and soil temperature and humidity, and lacks experimental verification and model support of a system. In practical researches, the following problems are common in the conventional silicate mineral chemical weathering leaching experimental device:\| (1) By adopting a manual liquid adding mode, the leaching solution amount is difficult to be matched with the natural precipitation condition; \| (2) Only is carried out at room temperature, lacks heating and temperature control functions, and cannot reflect the change of the real soil under the temperature and humidity conditions. \|[0004] The problems cause great deviation between laboratory simulated silicate mineral weathering experimental results and chemical weathering under actual natural conditions, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain. Therefore, development of a chemical weathering leaching experimental device capable of simulating silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment is needed to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners and novel mineral fertilizers.\|DISCLOSURE\|Disclosure of Invention\|[0005] Based on the problem that the laboratory simulation silicate mineral weathering experimental result in the prior art has larger deviation from the chemical weathering under the actual natural condition, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain, the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions, which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable temperature and humidity conditions, so as to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and provide scientific basis and experimental support for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers.\|[0006] In order to achieve the purpose, the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided, and comprises:\| The temperature control device comprises a support frame and an incubator device arranged on the support frame; \| The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; \| a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; \| a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and \|And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.\|[0007] Further, the rainfall simulation device comprises a spraying component arranged at the open top of the leaching column, a syringe pump mechanism for drawing and pumping leaching solution, a liquid delivery pipe for connecting the spraying component with a liquid outlet port of the syringe pump mechanism, a water inlet pipe for connecting a liquid inlet port of the syringe pump mechanism with a liquid storage container, and a supporting seat for supporting the syringe pump mechanism, wherein the syringe pump mechanism is fixedly arranged on the supporting seat, the leaching device for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity further comprises a driving device for driving the syringe pump mechanism to draw and pump leaching solution, a first valve arranged at the liquid inlet port of the syringe pump mechanism and a second valve arranged at the liquid outlet port of the syringe pump mechanism, the driving device is arranged on the supporting seat, and the driving device, the first valve and the second valve can be controlled to work and are respectively and electrically connected with the controller.\|[0008] Further, the injection pump mechanism comprises an injection cylinder, a first piston, a second piston, a push-pull rod, a first linkage rod, a sleeve and a second linkage rod, wherein the two ends of the injection cylinder are respectively in an opening shape, the first piston is arranged in the injection cylinder in a sliding mode, the second piston is arranged in the injection cylinder in a sliding mode, the push-pull rod is used for driving the first piston to move along the axial direction of the injection cylinder, the first linkage rod is connected with one end, far away from the first piston, of the push-pull rod, the sleeve is used for driving the second piston to move along the axial direction of the injection cylinder, the second linkage rod is connected with one end, far away from the second piston, of the sleeve, a first sliding hole is formed in the second piston, the outer peripheral surface of the push-pull rod is in interference contact with the inner hole wall of the first sliding hole, the sleeve can be sleeved on the push-pull rod in an axial sliding mode, and the first linkage rod and the second linkage rod are respectively connected with the driving device.\|[0009] Further, the driving device comprises a driving assembly, a connecting rod mechanism connecting the first linkage rod with the second linkage rod, and a gear mechanism connecting the connecting rod mechanism with the driving assembly, wherein the gear mechanism comprises a first gear rotatably installed on the supporting seat and a second gear rotatably installed on the supporting seat, the first gear is meshed with the second gear, the first gear and/or the second gear are/is connected with the driving assembly so that the driving assembly can drive the first gear and the second gear to synchronously rotate, the connecting rod mechanism comprises a first driving rod fixedly connected with the first gear, a first connecting rod rotatably connecting the first end of the first driving rod with the first end of the first linkage rod, a second connecting rod rotatably connecting the second end of the first driving rod with the first end of the second linkage rod, a second driving rod fixedly connected with the second gear, a second connecting rod fixedly connected with the second end of the second driving rod, a second connecting rod fixedly connected with the second end of the second connecting rod, a second connecting rod with the second connecting rod, and a first connecting rod with the second connecting rod, and a second connecting rod with the second connecting rod, and the connecting rod with the second connecting rod with the first connecting rod and the second connecting rod with the second connecting rod.\|[0010] Further, the driving assembly comprises a first driving shaft arranged on the supporting seat in a rotating mode, a second driving shaft arranged on the supporting seat in a rotating mode, a driving motor fixedly installed on the supporting seat, a first synchronous belt wheel fixedly sleeved on the first driving shaft, a second synchronous belt wheel fixedly sleeved on the second driving shaft, a third synchronous belt wheel fixedly sleeved on a motor shaft of the driving motor, and a synchronous belt connecting the first synchronous belt wheel, the second synchronous belt wheel and the third synchronous belt wheel, wherein the driving motor is electrically connected with the controller.\|[0011] Further, a pressure sensor for detecting the leaching solution pressure in the injection cylinder is arranged in the injection cylinder, and the pressure sensor is electrically connected with the controller.\|[0012] Further, the leaching assembly further comprises a first mesh plate arranged in a leaching cavity in the leaching column and a first filter screen paved on the mesh plate, silicate rock powder in the leaching column forms a columnar rock body, and the bottom end of the columnar rock body is supported on the first mesh plate.\|[0013] Further, the incubator device includes the incubator that inside was equipped with the constant temperature chamber, set up in on the incubator in order to open or close selectively the chamber door in constant temperature chamber, set up in inside in order to realize the refrigerator of constant temperature intracavity temperature regulation of incubator, and set up in inside air cycle and the heating mechanism of incubator, air cycle and the heating mechanism can be accelerated air cycle flow in the constant temperature chamber, and heat air in the constant temperature chamber, the controller can be according to humidity and the temperature control that temperature and humidity sensor detected the refrigerator air cycle and the heating mechanism work, adjust the temperature in the constant temperature chamber, so that the temperature in the constant temperature chamber keeps in the preset temperature range of 0 ℃ to 25 ℃.\|[0014] Further, the air circulation and heat supply mechanism comprises a circulation air channel arranged in the constant temperature cavity, an air inlet pipe communicated with an air inlet of the circulation air channel, an air return pipe communicated with an air return port of the circulation air channel, a heating component arranged in the circulation air channel and a circulation fan arranged in the circulation air channel, wherein the heating component comprises a plurality of heating pipes which are transversely arranged.\|[0015] Further, the spraying assembly comprises a spray head connected with the infusion tube and a spraying support for supporting the spray head on the support frame and/or at the top end of the leaching column, and the spraying support is detachably connected with the support frame and/or the leaching column.\|[0016] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:\| According to the leaching equipment for simulating chemical weathering under the natural temperature and humidity conditions of silicate rock powder, which is disclosed by the embodiment of the invention, the actual natural rainfall and the natural saline-alkali soil temperature and humidity conditions can be simulated, and mineral chemical weathering of the precipitation amount is simulated according to the actual temperature and humidity of the saline-alkali soil, so that the chemical weathering process of silicate minerals in the natural environment of the saline-alkali soil is simulated truly, the true accuracy of the silicate mineral chemical weathering experimental result is improved, and the reliable weathering reaction, salt replacement and carbon fixing process data of the silicate minerals in the saline-alkali soil are obtained, so that scientific basis and experimental support are provided for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers. \|DRAWINGS DESCRIPTION\|[0017] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0018] FIG. 1 is a schematic diagram of a three-dimensional structure of leaching equipment simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions;\| FIG. 2 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 3 is a schematic top view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 4 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 5 is an assembly diagram of a rainfall simulation device and a driving device according to an embodiment of the present invention in a first working state; \| FIG. 6 is a schematic cross-sectional view of the structure shown in FIG. 5; \| fig. 7 is an assembly diagram of the rainfall simulation device and the driving device provided by the embodiment of the invention in a second working state; \| FIG. 8 is a schematic top view of the structure shown in FIG. 7; \| FIG. 9 is a schematic cross-sectional view of the structure shown in FIG. 7; \| Fig. 10 is a schematic perspective view of a leaching assembly according to an embodiment of the present invention; \| FIG. 11 is a schematic cross-sectional view of a leaching assembly according to an embodiment of the present invention; \| FIG. 12 is an exploded view of a leaching assembly provided by an embodiment of the present invention; \| FIG. 13 is a schematic perspective view of an incubator assembly according to an embodiment of the present invention; \| Fig. 14 is a schematic cross-sectional structure of an incubator assembly according to an embodiment of the present invention. \|[0019] Wherein, each reference sign in the figure:\| 1-temperature control device, 11-supporting frame, 12-incubator device, 121-incubator, 122-oven door, 123-refrigerator, 124-air circulation and heat supply mechanism, 1241-circulation air duct, 1242-muffler, 1243-heating assembly, 1244-circulation fan, 1245-air inlet pipe, 125-mounting hole and 126-observation window; \| 2-leaching components, 21-leaching columns, 22-liquid collecting containers, 23-liquid discharge pipes, 24-first mesh plates, 25-first filter screens, 26-second filter screens and 27-second mesh plates; \| 3-a rainfall simulation device, 31-a spray assembly, 311-a spray head, 312-a spray bracket, 32-a syringe pump mechanism, 321-a syringe, 322-a first piston, 323-a second piston, 324-a push-pull rod, 325-a first linkage rod, 326-a sleeve, 327-a second linkage rod, 33-a transfusion tube, 34-a water inlet tube and 35-a supporting seat; \| 4-drive means, 41-drive assembly, 411-first drive shaft, 412-second drive shaft, 413-drive motor, 414-first timing pulley, 415-second timing pulley, 416-third timing pulley, 417-timing belt, 418-motor shaft, 42-link mechanism, 421-first drive rod, 422-first link, 423-second link, 424-second drive rod, 425-third link, 426-fourth link, 43-gear mechanism, 431-first gear, 432-second gear; \| 5-fixed support, 6-bolt piece, 7-liquid storage space, 8-columnar rock mass and 9-controller. \|INVENTION MODE\|Detailed Description\|[0020] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0021] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, features defining "first," "second," and "third" may explicitly or implicitly include one or more such features. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0022] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.\|[0023] Referring to fig. 1 to 14, a description will now be given of an leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention. Referring to fig. 1, fig. 2, fig. 3 and fig. 4 in combination, the leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions provided by the embodiment of the invention comprises a temperature control device 1, a leaching assembly 2, a rainfall simulation device 3, a temperature and humidity sensor and a controller 9, wherein the temperature control device 1 comprises a support frame 11 and a constant temperature box device 12 arranged on the support frame 11. The leaching assembly 2 comprises a leaching column 21 arranged in the incubator device 12 and a liquid collecting container 22 arranged below the leaching column 21, wherein two axial ends of the leaching column 21 respectively extend out of the incubator device 12, the top end of the leaching column 21 is open, and a liquid discharging pipe 23 communicated with the liquid collecting container 22 is arranged at the bottom end of the leaching column 21. Wherein, the leaching column 21 is a column-shaped leaching container made of high-temperature resistant transparent plastic or high-temperature resistant transparent organic glass. The rainfall simulation device 3 is used for simulating rainfall so that the leaching solution can uniformly flow into silicate rock powder in the leaching column 21 through the top end opening of the leaching column 21. The temperature and humidity sensor is used for detecting the temperature and humidity of silicate rock powder in the leaching column 21 in real time, and a probe of the temperature and humidity sensor is inserted into the leaching column 21. It should be noted that, the temperature and humidity sensor is implemented by adopting the prior art, and its working principle and structure are well known to those skilled in the art, and are not described herein. The controller 9 is used for controlling the rainfall simulation device 3 and the incubator device 12 to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of the silicate rock powder in the leaching column 21 is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column 21 is maintained at 30-80%. It should be noted that the controller 9 may be, but is not limited to, a programmable logic controller.\|[0024] The basic working principle of the leaching equipment for simulating chemical weathering of silicate rock powder under the natural temperature and humidity condition is that silicate rock is crushed into silicate rock powder with the particle size of 0.1 micron, the silicate rock powder and a certain amount of saline-alkali soil are uniformly mixed and filled in a leaching column 21 of a leaching assembly 2, and a rainfall simulation device 3 is arranged at the opening at the top end of the leaching column 21. The simulated rainfall device 3 carries out real simulated rainfall characteristics on the leaching solution, so that the leaching solution can flow into the silicate rock powder in the leaching column 21 through the opening at the top end of the leaching column 21, the silicate rock powder in the leaching column 21 can be uniformly leached, disturbance on the silicate rock powder in the leaching column 21 is reduced, leaching efficiency and leaching effect of the silicate rock powder in the leaching column 21 are improved, and accuracy of silicate mineral chemical weathering experimental results is improved. In addition, during leaching, the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, and after the leaching solution permeates the silicate rock powder in the leaching column 21, the leaching solution is drained into the liquid collecting container 22 through the liquid drain pipe 23 at the bottom end of the leaching column 21. And, in the whole process of the chemical weathering experiment, the temperature in the incubator device 1 and the humidity in the leaching column 21 are detected in real time through the temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is less than 0 ℃, the controller 9 controls the heating component in the incubator device 1 to heat and work until the temperature in the incubator device 1 reaches 25 ℃, and the controller 9 controls the heating component in the incubator device 1 to stop heating and work. When the temperature in the oven apparatus 1 is greater than 25 ℃, the controller 9 controls the refrigerator in the oven apparatus 1 to operate until the temperature in the oven apparatus 1 reaches 25 ℃, and the controller 9 controls the refrigerator in the oven apparatus 1 to stop the cooling operation. The circulation is such that the temperature in the oven apparatus 1 is controlled within a preset temperature range of 0 to 25 ℃, thereby making the silicate rock powder in the leaching column 21 subjected to the chemical weathering simulation experiment under the temperature condition of 0 to 25 ℃. Of course, the controller 9 may also control the operation of the heating element and/or the refrigerator in the incubator apparatus 1 so that the temperature in the incubator apparatus 1 is stabilized at any one of the preset temperature values between 0 ℃ and 25 ℃ and so that the silicate powder in the leaching column 21 is subjected to chemical weathering simulation test under a specific temperature condition (e.g., 5 ℃, 10 ℃, 15 ℃, 20 ℃,25 ℃ or the like) between 0 ℃ and 25 ℃. Meanwhile, when the humidity in the leaching column 21 is less than 30%, the controller 9 controls the rainfall simulation device 3 to work, so that the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, until the humidity in the leaching column 21 reaches 80%, the controller 9 controls the rainfall simulation device 3 to stop working, and the circulation is performed in such a way that the humidity in the leaching column 21 is controlled within a preset humidity range of 30-80%, and thus chemical weathering simulation experiments are performed on the silicate rock powder in the leaching column 21 under a humidity condition of 30-80%. Therefore, the method can simulate the actual natural rainfall and the natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, simulate the mineral chemical weathering of the precipitation according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and improve the true accuracy of the silicate mineral chemical weathering experimental result so as to obtain the reliable weathering reaction, salt replacement and carbon fixation process data of the silicate minerals of the saline-alkali soil, thereby being beneficial to improving the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|[0025] Referring to fig. 2,3 and 4, in some embodiments, the rainfall simulation device 3 includes a spray assembly 31 disposed at an opening at a top end of the leaching column 21, a syringe pump mechanism 32 for drawing and pumping the leaching solution, a transfusion tube 33 connecting the spray assembly 31 and a liquid outlet port of the syringe pump mechanism 32, a water inlet pipe 34 for connecting a liquid inlet port of the syringe pump mechanism 32 with a liquid storage container, and a support seat 35 for supporting the syringe pump mechanism 32, the syringe pump mechanism 32 is fixedly mounted on the support seat 35, the leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions further includes a driving device 4 for driving the syringe pump mechanism 32 to draw and pump the leaching solution, a first valve disposed at the liquid inlet port of the syringe pump mechanism 32 and a second valve disposed at the liquid outlet port of the syringe pump mechanism 32, the driving device 4 is disposed on the support seat 35, and the controller 9 can control the driving device 4, the first valve and the second valve to work, and the driving device 4, the first valve and the second valve are respectively electrically connected with the controller 9. It will be appreciated that in some of these embodiments the first valve 9 and the second valve 10 are solenoid valves. By the above arrangement, the silicate rock is crushed into silicate rock powder having a particle size of 0.1 μm, the silicate rock powder is packed in the leaching column 21 of the leaching assembly 2, and the spraying assembly 31 is installed at the top end opening of the leaching column 21. When the injection pump mechanism 32 is required to be used for sucking the leaching solution from the liquid storage container under the negative pressure, the controller controls the first valve 9 to open the liquid inlet of the injection pump mechanism 32, the controller controls the second valve 10 to close the liquid outlet of the injection pump mechanism 32, the driving device 4 drives the injection pump mechanism 32 to suck the leaching solution from the liquid storage container under the negative pressure, until the leaching solution in the injection pump mechanism 32 is full, the controller controls the first valve 9 to close the liquid inlet of the injection pump mechanism 32, and the controller controls the second valve 10 to open the liquid outlet of the injection pump mechanism 32, the injection pump mechanism 32 can pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the simulated rainfall device 3 under the driving action of the driving device 4, the real rainfall simulation characteristic is realized, the uniformity of the silicate powder in the leaching column 21 is ensured, the silicate powder in the leaching column 21 is uniformly leached, the disturbance of the silicate powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate powder in the leaching column 21 are further improved, and the accuracy of silicate mineral chemical weathering experiment results is facilitated. In addition, during leaching, the leaching solution of the silicate powder in the leaching column 21 is uniformly sprayed to the leaching column 21 at a certain flow rate through the spraying assembly 31, and is drained into the liquid collecting container 22 through the drain pipe 23 at the bottom end of the leaching column 21 after penetrating the silicate powder in the leaching column 21.\|[0026] Therefore, in the leaching device for simulating chemical weathering of silicate rock powder under the natural temperature and humidity conditions, when the controller controls the first valve 9 to be opened and the second valve 10 to be closed, the driving device 4 can drive the injection pump mechanism 32 to draw the leaching solution from the liquid storage container through negative pressure until the injection pump mechanism 32 draws enough leaching solution, then the controller controls the first valve 9 to be closed and the second valve 10 to be opened, the injection pump mechanism 32 can continuously pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the rainfall simulator 3 under the driving action of the driving device 4, the real rainfall simulation characteristic of the spraying assembly 31 of the rainfall simulator 3 is adopted to ensure the uniformity of the leaching solution flowing into the silicate rock powder in the leaching column 21, so that the silicate rock powder in the leaching column 21 can be uniformly leached, the disturbance of the silicate rock powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate rock powder in the leaching column 21 are improved, and the accuracy of the silicate mineral chemical weathering experiment result is improved.\|[0027] Referring to fig. 2,6 and 9 in combination, in some embodiments, the syringe pump mechanism 32 includes a syringe 321, a first piston 322, a second piston 323, a push-pull rod 324, a first linkage rod 325, a sleeve 326 and a second linkage rod 327, two ends of the syringe 321 are all open, the first piston 322 and the second piston 323 are respectively slidably disposed in the syringe 321, and when the first piston 322 and the second piston 323 are respectively slid to the openings at two ends of the syringe 321, a closed liquid storage space 7 for storing the shower solution can be formed in the syringe 321, and the liquid storage capacity of the liquid storage space 7 can be preset. The push-pull rod 324 is used for driving the first piston 322 to move along the axial direction of the injection cylinder 321, the sleeve 326 is used for driving the second piston 323 to move along the axial direction of the injection cylinder 321, and when the first piston 322 and the second piston 323 move away from each other along the axial direction of the injection cylinder 321, the solution can be pumped from the liquid storage container through the injection pump mechanism 32, and the pumped solution can be stored in the closed liquid storage space 7 between the first piston 322 and the second piston 323. When the first piston 322 and the second piston 323 move closer to each other in the axial direction of the syringe 321, the shower solution in the solution storage space 7 can be continuously pumped to the shower assembly 31 of the rainfall simulation device 3 by the syringe pump mechanism 32. The first linkage rod 325 is connected with one end of the push-pull rod 324 far away from the first piston 322, the second linkage rod 327 is connected with one end of the sleeve 326 far away from the second piston 323, the first linkage rod 325 and the second linkage rod 327 are respectively connected with the driving device 4, a first sliding hole for the push-pull rod 324 to pass through is arranged on the second piston 323, the outer peripheral surface of the push-pull rod 324 is in interference contact with the inner hole wall of the first sliding hole, and the sleeve 326 can be sleeved on the push-pull rod 324 in an axial sliding manner. When the driving device 4 drives the first linkage rod 325 and the second linkage rod 327, the sleeve 326 is sleeved on the push-pull rod 324 in a sliding manner along the axial direction, so that the first piston 322 and the second piston 323 can move towards or away from each other along the axial direction of the injection cylinder 321. It should be noted that, the liquid inlet port and the liquid outlet port are both disposed on the syringe 321, and the liquid inlet port and the liquid outlet port are respectively communicated with the liquid storage space 7.\|[0028] Referring to fig. 4, 5, 7 and 8 in combination, in some embodiments, the driving device 4 includes a driving assembly 41, a link mechanism 42 and a gear mechanism 43, the link mechanism 42 is used to connect the first link lever 325 with the second link lever 327, the gear mechanism 43 is used to connect the link mechanism 42 with the driving assembly 41, the gear mechanism 43 includes a first gear 431 rotatably mounted on the support seat 35 and a second gear 432 rotatably mounted on the support seat 35, the first gear 431 and the second gear 432 are the same in size and structure, the first gear 431 and the second gear 432 mesh, the first gear 431 and the second gear 432 are connected with the driving assembly 41, and one gear of the first gear 431 and the second gear 432 may be connected with the driving assembly 41, so that the driving assembly 41 can drive the first gear 431 and the second gear 432 to rotate synchronously. The link mechanism 42 includes a first driving lever 421 fixedly coupled to a first gear 431, a first link 422 rotatably coupling a first end of the first driving lever 421 with a first end of a first link lever 325, a second link 423 rotatably coupling a second end of the first driving lever 421 with a first end of a second link lever 327, a second driving lever 424 fixedly coupled to a second gear 432, a third link 425 rotatably coupling a first end of the second driving lever 424 with a second end of the first link lever 325, a fourth link 426 rotatably coupling a second end of the second driving lever 424 with a first end of the second link lever 327, the lengths of the first link 422, the second link 423, the third link 425, and the fourth link 426 being equal, the length of the first link lever 325 being equal to the length of the second link lever 327, and the length of the first driving lever 421 being equal to the length of the second link lever 424. It should be noted that, two ends of the first link 422 are respectively rotatably connected to the first end of the first driving rod 421 and the first end of the first linkage rod 325 through a pivot, and two ends of the second link 423 are respectively rotatably connected to the second end of the first driving rod 421 and the second end of the first linkage rod 325 through a pivot. Through the above structure, the driving assembly 41 can synchronously drive the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321, and can improve the stability of the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321. In addition, the connecting rod mechanism 42 is driven by the rotation of the gear mechanism 43 to drive the first piston 322 and the second piston 323 to move close to each other along the axial direction of the injection cylinder 321, and the speed of the injection pump mechanism 32 for pumping the leaching solution can be controlled by controlling the rotation speed of the first gear 431 and/or the second gear 432, so that the leaching rate can be controlled and regulated according to the leaching experiment requirement.\|[0029] Referring to fig. 4, 5 and 7, in some embodiments, the driving assembly 41 includes a first driving shaft 411, a second driving shaft 412, a driving motor 413, a first synchronous belt 417 wheel 414, a second synchronous belt 417 wheel 415, a third synchronous belt 417 wheel 416 and a synchronous belt 417, the first driving shaft 411 and the second driving shaft 412 are respectively rotatably disposed on the supporting seat 35, the driving motor 413 is fixedly mounted on the supporting seat 35, the first synchronous belt 417 wheel 414 is fixedly sleeved on the first driving shaft 411, the second synchronous belt 417 wheel 415 is fixedly sleeved on the second driving shaft 412, the third synchronous belt 417 wheel 416 is fixedly sleeved on a motor shaft 418 of the driving motor 413, and the synchronous belt 417 connects the first synchronous belt 417 wheel 414, the second synchronous belt 417 wheel 415 and the third synchronous belt 417 wheel 416, and the driving motor 413 is electrically connected with the controller. Through the above structure arrangement, under the driving action of the driving motor 413, the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 synchronously rotate, so as to drive the gear mechanism 43 to rotate, and the gear mechanism 43 drives the first piston 322 and the second piston 323 to move close to or far away from each other along the axial direction of the injection cylinder 321 through the link mechanism 42, so that the injection pump mechanism 32 can finish the action of drawing and pumping the shower solution.\|[0030] Referring to fig. 2, 4 and 5, in some embodiments, the first gear 431 is fixedly sleeved on the first driving shaft 411, the second gear 432 is fixedly sleeved on the second driving shaft 412, and the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are arranged in an isosceles triangle, so that the distance between the first driving shaft 411 and the second driving shaft 412, the distance between the first driving shaft 411 and the motor shaft 418 of the driving motor 413, and the distance between the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are all equal. By the above arrangement, the stability of the movement of the first piston 322 and the second piston 323 in the axial direction of the syringe 321 toward each other or away from each other can be improved.\|[0031] In some embodiments, a pressure sensor for detecting leaching liquid pressure inside the syringe 321 is disposed in the syringe 321, and the pressure sensor is electrically connected to the controller. The controller can control the rotation speed of the driving motor 413 to control the rotation speed of the first gear 431 and/or the second gear 432 according to the pressure detected by the pressure sensor, so as to control the speed of the injection pump mechanism 32 for pumping the leaching solution, thereby being convenient for controlling and adjusting the leaching rate according to the leaching experiment requirement.\|[0032] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a first mesh plate 24 disposed in the leaching chamber in the leaching column 21 and a first filter screen 25 laid on the mesh plate, silicate rock powder in the leaching column 21 forms a columnar rock body 8, and a bottom end of the columnar rock body 8 is supported on the first mesh plate 24. Through the structure setting, through adopting the first mesh board 24 that plastics or metal etc. made to the silicate rock powder in the leaching column 21 to form column rock mass 8 bottom formation support, the leaching solution after the rethread first filter screen 25 on the first mesh board 24 filters, can prevent effectively that the silicate rock powder in the leaching column 21 from forming column rock mass 8 bottom and collapsing, ensure simultaneously that the leaching solution that liquid collecting container 22 collected does not contain silicate rock powder, be favorable to improving the accuracy of leaching experiment. The mesh size of the first screen 25 is smaller than the particle size of the silicate powder.\|[0033] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a second screen 26 disposed on top of the columnar rock mass 8 and a second mesh plate 27 disposed over the second screen 26. By paving the second filter screen 26 on the top end of the columnar rock body 8 formed by silicate rock powder in the leaching column 21 and covering the second filter screen 26 with a second mesh plate 27 made of hard materials such as plastics or metals, the integrity of the top of the columnar rock body 8 is prevented from being damaged due to the fact that the concentrated impact of leaching solution water flows form a dent.\|[0034] Referring to fig. 2 and 4 in combination, in some embodiments, spray assembly 31 includes a spray head 311 coupled to a fluid line 33, and a spray bracket 312 for supporting spray head 311 on support frame 1 and/or on the top of leaching column 21, spray bracket 312 being removably coupled to support frame 1 and/or leaching column 21. It should be noted that the spray head 311 may be, but is not limited to, an atomizing spray head 311. In actual operation, the speed of the driving motor 413 is controlled, and various rainfall is simulated by adopting the atomizing nozzle 311, so that silicate rock powder in the leaching column 21 forms a columnar rock body 8, and the problems that the soil column structure is damaged and the leaching speed of water is influenced due to the fact that water flow impacts to form a recess are avoided.\|[0035] Referring to fig. 13 and 14 in combination, in some embodiments, the incubator apparatus 12 includes an incubator 121 having a constant temperature chamber therein, a door 122 provided on the incubator 121 to selectively open or close the constant temperature chamber, a refrigerator 123 provided inside the incubator 121 to achieve temperature adjustment in the constant temperature chamber, and an air circulation and heat supply mechanism 124 provided inside the incubator 121, the air circulation and heat supply mechanism 124 being capable of accelerating the air circulation flow in the constant temperature chamber and heating the air in the constant temperature chamber, and the controller 9 being capable of controlling the operation of the refrigerator 123, the air circulation and heat supply mechanism 124 according to the humidity and temperature detected by the temperature and humidity sensor to adjust the temperature in the constant temperature chamber so as to maintain the temperature in the constant temperature chamber within a preset temperature range of 0 to 25 ℃ or to any specific temperature value between 0 to 25 ℃. The incubator 121 is provided with a mounting hole 125 for accommodating and mounting the leaching column 21, and the outer side wall of the leaching column 21 is in airtight contact with the inner hole wall of the mounting hole 125. The door 122 is provided with a transparent observation window 126 made of high temperature resistant glass so as to observe leaching conditions in the leaching column 21 inside the incubator 121. In the whole process of chemical weathering experiment, the temperature in the incubator device 1 is detected in real time through a temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is smaller than 0 ℃, the controller 9 controls the refrigerator 123 to be closed and controls the air circulation and heat supply mechanism 124 in the heat preservation 121 to work, and the air circulation and heat supply mechanism 124 accelerates the air circulation flow in the constant temperature cavity and heats the air in the constant temperature cavity, so that the temperature in the constant temperature cavity of the incubator 121 is quickly increased until the temperature in the constant temperature cavity of the incubator 121 reaches 25 ℃, and the controller 9 controls the air circulation and heat supply mechanism 124 in the incubator device 1 to stop heating work. If the temperature in the constant temperature chamber of the incubator 121 is higher than 25 ℃, the controller 9 controls the refrigerator 123 to operate and controls the air circulation and heating mechanism 124 to stop operating, so that the temperature in the constant temperature chamber is reduced by between 0 and 25 ℃. By means of the circulation, the temperature in the heat preservation box 121 can be controlled within a preset temperature range of 0-25 ℃, so that silicate rock powder in the leaching column 21 is subjected to chemical weathering simulation experiments under the temperature condition of 0-25 ℃ to simulate actual natural rainfall and natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, mineral chemical weathering of simulated precipitation is performed according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and the actual accuracy of silicate mineral chemical weathering experiment results is improved.\|[0036] Referring to fig. 13 and 14 in combination, in some embodiments, the air circulation and heat supply mechanism 124 includes a circulation duct 1241 disposed in the constant temperature chamber, an air inlet pipe 1245 connected to an air inlet of the circulation duct 1241, an air return pipe 1242 connected to an air return port of the circulation duct 1241, a heating assembly 1243 disposed in the circulation duct 1241, and a circulation fan 1244 disposed in the circulation duct 1241, the heating assembly 1243 including a plurality of heating pipes disposed transversely. When the air circulation and heat supply mechanism 124 works, air in the constant temperature cavity is led into the circulation air channel 1241 by the air inlet pipe 1245 under the action of the circulation fan 45, the air in the circulation air channel 1241 is heated by the heating component 1244 and then becomes hot air, and the hot air in the circulation air channel 1241 flows back to the constant temperature cavity by the air return pipe 1243, so that the air circulation and heat supply mechanism 124 can be used for quickly heating the air in the constant temperature cavity.\|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.	Family Number\|(117662153)\|117662153\|Object of Invention\|(CN121454002 A)\|In order to achieve the purpose , the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided , and comprises : \|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions , and belongs to the technical fields of enhanced rock weathering carbon fixation , mineral fertilizer development and saline soil improvement and management . \|Abstract\|(CN121454002 A)\|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions , and belongs to the technical fields of rock weathering and carbon sequestration enhancement , mineral fertilizer development and saline soil improvement and treatment . The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions . The leaching equipment comprises a temperature control device , a leaching assembly , a rainfall simulation device , a temperature and humidity sensor and a controller , wherein the temperature control device comprises a support frame and a constant temperature box device arranged on the support frame . The leaching assembly comprises a leaching column arranged in the constant - temperature box device and a liquid collecting container arranged below the leaching column . The equipment can simulate a chemical weathering leaching experiment of silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment so as to really simulate a chemical weathering process of the silicate minerals in a natural environment of saline - alkali soil ; scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners , novel mineral fertilizers and saline - alkali soil improvement . \|Title\|(CN121454002 A)\|Leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions \|Advantages / Prev. Drawbacks\|(CN121454002 A)\|( . . . ) actual natural condition , and reliable silicate mineral weathering rate , nutrient release and carbon fixing process data are difficult to obtain , the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions , which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable ( . . . ) \|Independent Claims\|(CN121454002 A)\|1. An leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions , comprising : ( . . . ) a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column ; a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time , a probe of the temperature and humidity sensor being inserted into the leaching column , and And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor , so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%. \|	Analysis of biological materials	G01N-033/00\|G01N-033/00/98\|G01N-033/24		G01N-033/00\|G01N-033/00/98\|G01N-033/24	G01N-033/00\|G01N-033/24	G01N-033/00\|G01N-033/24										PENDING	(CN121454002)\|PENDING	ALIVE	(CN121454002)\|ALIVE	(CN121454002)\|LEGAL DETAILS FOR CN121454002\|Actual or expected expiration date=2045-11-20\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-11-20\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202511707827\|Application date=2025-11-20\|Standardized application number=2025CN-1707827\|Event publication date=2026-02-03\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN121454002\|Publication stage code=A\|Publication date=2026-02-03\|Standardized publication number=CN121454002\|Event publication date=2026-02-03\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2026-02-24\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN121454002)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKc0O21wABuVOlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080718408&ekey=2075&xpn=CN121454002&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=G2LF5CjifuL%252Fkpe3oMQTWZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN121454002)\|CN	(CN121454002)\|NAME=LANZHOU UNIVERSITY , COUNTRY=CN		(CN121454002)\|NAME=HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=41028	(CN121454002)\|CN	(CN121454002)\|NAME=ZHANG JIETANG, COUNTRY=CN \|NAME=LI XINGYUAN\|NAME=GOU XIAOHUA	(CN121454002)\|14	1	1					(CN121454002)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2026-02-03\|Gazette number: GAZNUM=42-0601\|Number of Pages: NPAGES=23\|		(CN121454002)\|CHINESE (CHI)	(CN121454002)\|Patent	Titre: (CN121454002)\|Leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions Résumé: (CN121454002)\|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, and belongs to the technical fields of rock weathering and carbon sequestration enhancement, mineral fertilizer development and saline soil improvement and treatment. The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions. The leaching equipment comprises a temperature control device, a leaching assembly, a rainfall simulation device, a temperature and humidity sensor and a controller, wherein the temperature control device comprises a support frame and a constant temperature box device arranged on the support frame. The leaching assembly comprises a leaching column arranged in the constant-temperature box device and a liquid collecting container arranged below the leaching column. The equipment can simulate a chemical weathering leaching experiment of silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment so as to really simulate a chemical weathering process of the silicate minerals in a natural environment of saline-alkali soil; scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners, novel mineral fertilizers and saline-alkali soil improvement.	4	Abstract	gpt-4o-mini	yes	The article describes leaching equipment designed to simulate chemical weathering of silicate rocks, which is directly related to enhanced weathering and carbon sequestration.
2	US63/213,398\|US63/213,398P\|US63/289,395\|US63/289,395P\|EP22829238\|US17/846,838\|US63/322,672\|US63/322,672P\|WOUS2022/034546\|US18/128,583\|US18/435,492\|US19/335,929	US19/335,929\|US18/435,492\|HK42023083673\|US18/128,583\|WOUS2022/034546\|HK62023083672\|BR112023023226\|EP22829238\|EP23199092\|AU2022299180\|CA3207124\|US17/846,838	US20260016458\|BR112023023226\|EP4256520\|EP4256520\|US12422425\|EP4256520\|AU2022299180\|US20240264139\|EP4276752\|US11921098\|BR112023023226\|HK40094979\|HK40095252\|EP4276752\|BR112023023226\|EP4256520\|US20230273174\|AU2022299180\|US11644454\|CA3207124\|WO2022/271842\|US20220404329	103013820	US20260016458 A1 2026-01-15 [US20260016458]\|US12422425 B2 2025-09-23 [US12422425]\|US20240264139 A1 2024-08-08 [US20240264139]\|HK40094979 A 2024-01-26 [HK40094979]\|US11921098 B2 2024-03-05 [US11921098]\|US20230273174 A1 2023-08-31 [US20230273174]\|WO2022/271842 A1 2022-12-29 [WO2022271842]\|HK40095252 A 2024-01-26 [HK40095252]\|BR112023023226 B1 2026-01-13 [BR112023023226]\|BR112023023226 A2 2024-01-30 [BR112023023226]\|BR112023023226 A0 2023-11-14 [BR112023023226]\|EP4256520 B1 2025-12-10 [EP4256520]\|EP4256520 C0 2025-12-10 [EP4256520]\|EP4256520 A4 2024-11-06 [EP4256520]\|EP4256520 A1 2023-10-11 [EP4256520]\|EP4276752 A3 2024-07-17 [EP4276752]\|EP4276752 A2 2023-11-15 [EP4276752]\|AU2022299180 A9 2024-10-24 [AU2022299180]\|AU2022299180 A1 2023-07-13 [AU2022299180]\|CA3207124 A1 2022-12-29 [CA3207124]\|US11644454 B2 2023-05-09 [US11644454]\|US20220404329 A1 2022-12-22 [US20220404329]	2021-06-22\|2021-12-14\|2022-03-23\|2022-06-22\|2023-03-30\|2024-02-07\|2025-09-22	2025-09-22\|2024-02-07\|2023-12-05\|2023-03-30\|2022-06-22\|2023-12-05\|2022-06-22\|2022-06-22\|2022-06-22\|2022-06-22\|2022-06-22\|2022-06-22	2026-01-15\|2026-01-13\|2025-12-10\|2025-12-10\|2025-09-23\|2024-11-06\|2024-10-24\|2024-08-08\|2024-07-17\|2024-03-05\|2024-01-30\|2024-01-26\|2024-01-26\|2023-11-15\|2023-11-14\|2023-10-11\|2023-08-31\|2023-07-13\|2023-05-09\|2022-12-29\|2022-12-29\|2022-12-22	(EP4256520)\|2025-12-10\|\|(US12422425)\|2025-09-23\|(US11921098)\|2024-03-05\|(US11644454)\|2023-05-09\|\|\|(BR112023023226)\|2026-01-13\|\|\|\|	(EP4256520)\|2042-06-22\|(EP4276752)\|2042-06-22\|(US12422425)\|2042-06-22\|(US11921098)\|2042-06-22\|(US11644454)\|2042-06-22\|(US20260016458)\|2042-06-22\|(WO2022/271842)\|2024-12-22\|(BR112023023226)\|2042-06-22\|(AU2022299180)\|2042-06-22\|(HK40095252)\|2042-06-22\|(HK40094979)\|2043-12-05\|(CA3207124)\|2042-06-22	(EP4256520)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering	(EP4256520)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.	EION	(EP4256520)\|Eion Corp.\|(EP4256520)\|Eion Corp. ([US])\|(EP4256520)\|Eion Corp.\|(EP4256520)\|Eion Corp. ([US])\|(EP4276752)\|Eion Corp. ([US])\|(EP4276752)\|Eion Corp. ([US])\|(US12422425)\|Eion Corp. ([US])\|(US20240264139)\|Eion Corp. ([US])\|(US11921098)\|Eion Corp. ([US])\|(US20230273174)\|Eion Corp. ([US])\|(US11644454)\|Eion Corp. ([US])\|(US20220404329)\|Eion Corp. ([US])\|(US20260016458)\|Eion Corp. ([US])\|(WO2022/271842)\|EION CORP. ([US])\|(BR112023023226)\|CORP EION ([US])\|(BR112023023226)\|CORP EION ([US])\|\|(AU2022299180)\|EION CORP.\|(AU2022299180)\|EION CORP.\|(HK40095252)\|Eion Corp ([US])\|(HK40094979)\|Eion Corp ([US])\|(CA3207124)\|EION CORP. ([US])	WOLF ADAM\|CHANG ELLIOT SUK-HYUN\|TANK ALAN ROBERT	(EP4256520)\|WOLF, Adam\|CHANG, Elliot Suk-Hyun\|TANK, Alan Robert\|(EP4256520)\|WOLF, Adam\|CHANG, Elliot Suk-Hyun\|TANK, Alan Robert\|(EP4256520)\|WOLF, Adam\|CHANG, Elliot Suk-Hyun\|TANK, Alan Robert\|(EP4256520)\|WOLF, Adam\|CHANG, Elliot Suk-Hyun\|TANK, Alan Robert	(EP4256520)\|Dragotti & Associati S.P.A. ([IT])\|Reg. Nb: 101869514\|(EP4276752)\|Dragotti & Associati S.R.L. ([IT])\|Reg. Nb: 101869514\|(US12422425)\|Frost Brown Todd LLP\|VanDrake, III Vance V.\|Johnson Alexander J.\|(US11921098)\|Frost Brown Todd LLP\|VanDrake, III Vance V.\|Johnson Alexander J.\|(US11644454)\|Ulmer & Berne LLP\|Van Drake, III Vance V.\|Johnson Alexander J.\|(WO2022/271842)\|FALK, Daniel T. et al. ([US])\|(AU2022299180)\|AJ Pietras IP Limited ([NZ])\|(HK40095252)\|HNC INNOVATION LIMITED ([HK])\|(HK40094979)\|HNC INNOVATION LIMITED ([HK])\|(CA3207124)\|BURNET, DUCKWORTH & PALMER LLP ([CA])	(EP4256520)\|This is a contrast with measurement schemes for soil organic carbon, in which the landowner or other interested party has an information advantage in terms of where or when to sample, which could be used to achieve a particular carbon measurement objective (high or low).\|VM2 may have an advantage over VM1 in not requiring tracking of a specific location for recovering the sampling column.\|Verification methodology 1 has the advantage that it can provide a direct measure of carbon flux and employs a measurement technique that is mature.\|The potential for ERW as a commercial enterprise is limited by some fundamental issues:\|	(EP4256520)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring the immobile trace elements in a soil sample after application of the mineral amendment to verify application of the mineral amendment, characterized in that the method comprises the steps of: determining the amount of the mineral amendment added to the soil sample, determining the amount of measured divalent cations in the soil sample, determining the fractional carbon dioxide removal by comparing the applied divalent cations to the measured divalent cations in the soil sample.\|	(EP4276752)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|	(EP4276752)\|ENHANCED ROCK(100,2)\|MINERAL AMENDMENT(100,2)\|REMOVING CARBON(100,1)\|VERIFICATION(100,1)\|ENHANCED ROCK WEATHERING(82,1)\|IMMOBILE TRACE ELEMENT(35,1)\|\|(EP4276752)\|ENHANCED ROCK(100,2)\|MINERAL AMENDMENT(100,2)\|REMOVING CARBON(100,1)\|VERIFICATION(100,1)\|ENHANCED ROCK WEATHERING(82,1)\|IMMOBILE TRACE ELEMENT(35,1)\|\|(US12422425)\|MINERAL AMENDMENT(100,22)\|VERIFICATION(100,17)\|REMOVING CARBON(100,12)\|ENHANCED ROCK(100,8)\|COMMINUTED SILICATE MINERAL(68,3)\|SILICATE MINERAL AGGLOMERATION(52,2)\|ENHANCED ROCK WEATHERING(46,2)\|INTERESTED PARTY(45,1)\|RECOVERING SAMPLING COLUMN(38,1)\|FUNDAMENTAL ISSUE(37,1)\|CARBON MEASUREMENT OBJECTIVE(25,1)\|LANDOWNER(23,1)\|SLOW RELEASE ACIDIFIER(22,3)\|IMMOBILE TRACE ELEMENT(21,25)\|COMMERCIAL ENTERPRISE(17,1)\|GIBBSITE(15,2)\|BINDER(14,3)\|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)\|NEODYMIUM(12,11)\|BRUKER PROPRIETARY GEO CALIBRATION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|LANTHANUM(11,9)\|SAMARIUM(11,8)\|SCANDIUM(11,8)\|YTTERBIUM(11,8)\|GADOLINIUM(11,7)\|PRASEODYMIUM(11,6)\|BERYLLIUM(11,2)\|GERMANIUM(11,2)\|RUBIDIUM(11,2)\|ZIRCONIUM(11,2)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|DRAWDOWN CALCULATION(10,4)\|ANDTHE TRANSITION METAL(10,1)\|AVERAGE PARTICLE SIZE(9,4)\|ERW(9,4)\|BLAST FURNACE SLAG(9,2)\|CESIUM(9,2)\|CHROMIUM(9,2)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|RIGOROUS QUANTIFICATION(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|BIOLOGICAL DERIVED COMPONENT(9,1)\|PELLETIZED MINERAL AMENDMENT(9,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|GYPSUM(8,3)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|NONLIMITING CANDIDATE(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|NEGATIVELY CHARGED BICARBONATE HCO(8,1)\|STERILIZED SOIL BEAKER(8,1)\|TRANSITION METAL(7,5)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|DISSOLUTION KINETICS(7,2)\|PHOSPHATE FERTILIZER(7,2)\|PULVERIZED SILICATE(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|CARBON FLUX(6,3)\|CHARGE IMBALANCE(6,2)\|INORGANIC ADDITIVE(6,2)\|MG PPM DETECTION(6,2)\|NEUTRAL GROUND(6,2)\|ROCK PARTICLE(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|AGGREGATED PELLET(6,1)\|AGLIME SUBSTITUTE(6,1)\|AGRICULTURAL SOILS(6,1)\|AGRONOMIC PERFORMANCE EXPECTATION(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|BIOFILM MEDIATING(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|DDIC DTA ESTIMATE(6,1)\|FORSTERITE METRIC TON(6,1)\|FORSTERITE TENDENCY(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INFERRED ION FLUX(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|INTENSE SCRUTINY(6,1)\|MARKETING COLLATERAL(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|NONPROFIT ORGANIZATION(6,1)\|OCEAN ACIDIFICATION(6,1)\|PELLET AGGLOMERATION(6,1)\|PHOSPHORUS ECOSYSTEM LOSS(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|PREAPPLICATION SOIL(6,1)\|PROTONATED MICROBE(6,1)\|PULVERIZED LIMESTONE(6,1)\|RENOWNED CHEMIST(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|REWET BIOMASS(6,1)\|RIGOROUS COMPLIANCE(6,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)\|SOIL CULTIVATED ZONE(6,1)\|SOIL GEOCHEMISTRY(6,1)\|SOIL HYDROLOGY(6,1)\|NACL SOLUTION(5,4)\|PROMETHIUM(5,4)\|PULVERIZATION(5,4)\|TRIPLICATE(5,4)\|CENTRIFUGE CELL(5,3)\|GROWING PLANT(5,2)\|AEROSOL SIZED PARTICLE(5,1)\|AGGREGATING GROUND MINERAL(5,1)\|ANALYTICAL LABORATORY(5,1)\|ANCIENT ROCK FORMATION(5,1)\|ANION CONSERVATION(5,1)\|CATEGORY REGULATION(5,1)\|CATION CONSERVATION(5,1)\|CLAUSE XII(5,1)\|DISSOLVE ALGINATE(5,1)\|DISSOLVED ALGINATE POWDER(5,1)\|DOWNSTREAM ECOSYSTEM(5,1)\|DOWNSTREAM WATERWAY(5,1)\|DTA DH INVERSE(5,1)\|DUST PREVALENCE(5,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)\|FUNGAL ADJUVANT(5,1)\|GROUND MINERAL AGGREGATION(5,1)\|KEY INSIGHT(5,1)\|MICROBIAL CATION EXCHANGER(5,1)\|MINERAL ADJUVANT(5,1)\|MINERAL TON HECTARE(5,1)\|NUTRIENT AVAILABILITY(5,1)\|PELLET DISSOLUTION(5,1)\|PHOSPHATE ZINC PRECIPITATE(5,1)\|PROGRESS FRACTIONATION(5,1)\|QUASI GOVERNMENTAL REGULATOR(5,1)\|RESERVOIR GEOLOGY(5,1)\|SOIL STERILIZATION(5,1)\|SPECIALIZED TOOL(5,1)\|STEAM STERILIZATION(5,1)\|TECHNO ECONOMIC MODELING(5,1)\|ULTIMATE PRICE(5,1)\|UREY REACTION BASIC PREMISE(5,1)\|V MONTE CARLO SIMULATION(5,1)\|VERIFICATION VERSION(5,1)\|VERIFIED ENHANCED ROCK(5,1)\|VOLUNTARY MARKET(5,1)\|RARE EARTH ELEMENT(4,18)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DISSOLUTION ENHANCING(4,1)\|DIVALENT MG(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|LB BROTH(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|PULVERIZED MG(4,1)\|REACTION THERMODYNAMICS(4,1)\|SECURITIZED CARBON REMOVAL(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|UNSEALING SAMPLE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|XRF ANALYSIS(4,1)\|K2H(3,4)\|BAG(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|T N(2,9)\|ANALYTICAL CHEMISTRY(2,3)\|K1H(2,3)\|LYSE(2,3)\|SOIL SAMPLE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|COMPUTING V(2,1)\|CONFIDENCE(2,1)\|CREATED VOID SPACE(2,1)\|DCREMAIN(2,1)\|\|(US20240264139)\|MINERAL AMENDMENT(100,22)\|VERIFICATION(100,17)\|REMOVING CARBON(100,12)\|ENHANCED ROCK(100,8)\|COMMINUTED SILICATE MINERAL(68,3)\|SILICATE MINERAL AGGLOMERATION(57,3)\|ENHANCED ROCK WEATHERING(46,2)\|INTERESTED PARTY(45,1)\|RECOVERING SAMPLING COLUMN(38,1)\|FUNDAMENTAL ISSUE(37,1)\|MINERAL TRANSFORMATION(31,2)\|CARBON MEASUREMENT OBJECTIVE(25,1)\|LANDOWNER(23,1)\|SLOW RELEASE ACIDIFIER(22,3)\|IMMOBILE TRACE ELEMENT(21,25)\|COMMERCIAL ENTERPRISE(17,1)\|GIBBSITE(15,2)\|BINDER(14,3)\|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)\|NEODYMIUM(12,11)\|BRUKER PROPRIETARY GEO CALIBRATION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|LANTHANUM(11,9)\|SAMARIUM(11,8)\|SCANDIUM(11,8)\|YTTERBIUM(11,8)\|GADOLINIUM(11,7)\|PRASEODYMIUM(11,6)\|BERYLLIUM(11,2)\|GERMANIUM(11,2)\|RUBIDIUM(11,2)\|ZIRCONIUM(11,2)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|DRAWDOWN CALCULATION(10,4)\|VROCK MONTE CARLO SIMULATION(10,1)\|AVERAGE PARTICLE SIZE(9,4)\|ERW(9,4)\|BLAST FURNACE SLAG(9,2)\|CASO(9,2)\|CESIUM(9,2)\|CHROMIUM(9,2)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|RIGOROUS QUANTIFICATION(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|BIOLOGICAL DERIVED COMPONENT(9,1)\|PELLETIZED MINERAL AMENDMENT(9,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|GYPSUM(8,3)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|NONLIMITING CANDIDATE(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|STERILIZED SOIL BEAKER(8,1)\|TRANSITION METAL(7,5)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|COMPUTING VROCK(7,2)\|DISSOLUTION KINETICS(7,2)\|PHOSPHATE FERTILIZER(7,2)\|PULVERIZED SILICATE(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|CARBON FLUX(6,3)\|CHARGE IMBALANCE(6,2)\|INORGANIC ADDITIVE(6,2)\|MG PPM DETECTION(6,2)\|NEUTRAL GROUND(6,2)\|ROCK PARTICLE(6,2)\|VROCK DOT PRODUCT(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|AGGREGATED PELLET(6,1)\|AGLIME SUBSTITUTE(6,1)\|AGRICULTURAL SOILS(6,1)\|AGRONOMIC PERFORMANCE EXPECTATION(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|BIOFILM MEDIATING(6,1)\|CO2 REAGENT AVAILABILITY(6,1)\|CO2 UPTAKE(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|DDIC DTA ESTIMATE(6,1)\|FORSTERITE METRIC TON(6,1)\|FORSTERITE TENDENCY(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INFERRED ION FLUX(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|INTENSE SCRUTINY(6,1)\|MARKETING COLLATERAL(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|NONPROFIT ORGANIZATION(6,1)\|OCEAN ACIDIFICATION(6,1)\|PELLET AGGLOMERATION(6,1)\|PHOSPHORUS ECOSYSTEM LOSS(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|PREAPPLICATION SOIL(6,1)\|PROTONATED MICROBE(6,1)\|PULVERIZED LIMESTONE(6,1)\|PULVERIZED MG2SIO(6,1)\|RENOWNED CHEMIST(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|REWET BIOMASS(6,1)\|RIGOROUS COMPLIANCE(6,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)\|SOIL CULTIVATED ZONE(6,1)\|SOIL GEOCHEMISTRY(6,1)\|SOIL HYDROLOGY(6,1)\|NACL SOLUTION(5,4)\|PROMETHIUM(5,4)\|PULVERIZATION(5,4)\|TRIPLICATE(5,4)\|CENTRIFUGE CELL(5,3)\|BICARBONATE HCO3(5,2)\|GROWING PLANT(5,2)\|AEROSOL SIZED PARTICLE(5,1)\|AGGREGATING GROUND MINERAL(5,1)\|ANALYTICAL LABORATORY(5,1)\|ANCIENT ROCK FORMATION(5,1)\|ANION CONSERVATION(5,1)\|CATEGORY REGULATION(5,1)\|CATION CONSERVATION(5,1)\|CLAUSE XII(5,1)\|DIFFERENCE VROCK VECTOR(5,1)\|DIFFERENCE VSOIL VECTOR(5,1)\|DISSOLVE ALGINATE(5,1)\|DISSOLVED ALGINATE POWDER(5,1)\|DOWNSTREAM ECOSYSTEM(5,1)\|DOWNSTREAM WATERWAY(5,1)\|DTA DH INVERSE(5,1)\|DUST PREVALENCE(5,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)\|FUNGAL ADJUVANT(5,1)\|GROUND MINERAL AGGREGATION(5,1)\|KEY INSIGHT(5,1)\|MICROBIAL CATION EXCHANGER(5,1)\|MINERAL ADJUVANT(5,1)\|MINERAL TON HECTARE(5,1)\|NUTRIENT AVAILABILITY(5,1)\|PELLET DISSOLUTION(5,1)\|PHOSPHATE ZINC PRECIPITATE(5,1)\|PROGRESS FRACTIONATION(5,1)\|QUASI GOVERNMENTAL REGULATOR(5,1)\|RESERVOIR GEOLOGY(5,1)\|SOIL STERILIZATION(5,1)\|SPECIALIZED TOOL(5,1)\|STEAM STERILIZATION(5,1)\|TECHNO ECONOMIC MODELING(5,1)\|ULTIMATE PRICE(5,1)\|UREY REACTION BASIC PREMISE(5,1)\|VERIFICATION VERSION(5,1)\|VERIFIED ENHANCED ROCK(5,1)\|VOLUNTARY MARKET(5,1)\|RARE EARTH ELEMENT(4,18)\|AQUEOUS CO2(4,2)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DISSOLUTION ENHANCING(4,1)\|DIVALENT MG(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|H2CO SUM(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|LB BROTH(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|REACTION THERMODYNAMICS(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|UNSEALING SAMPLE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|XRF ANALYSIS(4,1)\|BAG(3,2)\|CO2 REMOVAL(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MG MINERAL(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|SOIL SAMPLE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|CO2 MOLECULAR MASS(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|\|(US11921098)\|MINERAL AMENDMENT(100,22)\|VERIFICATION(100,18)\|REMOVING CARBON(100,13)\|ENHANCED ROCK(100,9)\|SILICATE MINERAL AGGLOMERATION(66,2)\|COMMINUTED SILICATE MINERAL(57,3)\|ENHANCED ROCK WEATHERING(46,2)\|INTERESTED PARTY(45,1)\|RECOVERING SAMPLING COLUMN(38,1)\|FUNDAMENTAL ISSUE(37,1)\|MINERAL TRANSFORMATION(31,2)\|CARBON MEASUREMENT OBJECTIVE(25,1)\|LANDOWNER(23,1)\|SLOW RELEASE ACIDIFIER(22,3)\|IMMOBILE TRACE ELEMENT(21,25)\|COMMERCIAL ENTERPRISE(17,1)\|GIBBSITE(15,2)\|BINDER(14,3)\|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)\|NEODYMIUM(12,11)\|BRUKER PROPRIETARY GEO CALIBRATION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|LANTHANUM(11,9)\|SAMARIUM(11,8)\|SCANDIUM(11,8)\|YTTERBIUM(11,8)\|GADOLINIUM(11,7)\|PRASEODYMIUM(11,6)\|BERYLLIUM(11,2)\|GERMANIUM(11,2)\|RUBIDIUM(11,2)\|ZIRCONIUM(11,2)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|DRAWDOWN CALCULATION(10,4)\|VROCK MONTE CARLO SIMULATION(10,1)\|AVERAGE PARTICLE SIZE(9,4)\|ERW(9,4)\|BLAST FURNACE SLAG(9,2)\|CASO(9,2)\|CESIUM(9,2)\|CHROMIUM(9,2)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|RIGOROUS QUANTIFICATION(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|BIOLOGICAL DERIVED COMPONENT(9,1)\|PELLETIZED MINERAL AMENDMENT(9,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|GYPSUM(8,3)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|NONLIMITING CANDIDATE(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|STERILIZED SOIL BEAKER(8,1)\|TRANSITION METAL(7,5)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|COMPUTING VROCK(7,2)\|DISSOLUTION KINETICS(7,2)\|PHOSPHATE FERTILIZER(7,2)\|PULVERIZED SILICATE(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|CARBON FLUX(6,3)\|CHARGE IMBALANCE(6,2)\|INORGANIC ADDITIVE(6,2)\|MG PPM DETECTION(6,2)\|NEUTRAL GROUND(6,2)\|ROCK PARTICLE(6,2)\|VROCK DOT PRODUCT(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|AGGREGATED PELLET(6,1)\|AGLIME SUBSTITUTE(6,1)\|AGRICULTURAL SOILS(6,1)\|AGRONOMIC PERFORMANCE EXPECTATION(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|BIOFILM MEDIATING(6,1)\|CO2 REAGENT AVAILABILITY(6,1)\|CO2 UPTAKE(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|DDIC DTA ESTIMATE(6,1)\|FORSTERITE METRIC TON(6,1)\|FORSTERITE TENDENCY(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INFERRED ION FLUX(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|INTENSE SCRUTINY(6,1)\|MARKETING COLLATERAL(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|NONPROFIT ORGANIZATION(6,1)\|OCEAN ACIDIFICATION(6,1)\|PELLET AGGLOMERATION(6,1)\|PHOSPHORUS ECOSYSTEM LOSS(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|PREAPPLICATION SOIL(6,1)\|PROTONATED MICROBE(6,1)\|PULVERIZED LIMESTONE(6,1)\|PULVERIZED MG2SIO(6,1)\|RENOWNED CHEMIST(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|REWET BIOMASS(6,1)\|RIGOROUS COMPLIANCE(6,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)\|SOIL CULTIVATED ZONE(6,1)\|SOIL GEOCHEMISTRY(6,1)\|SOIL HYDROLOGY(6,1)\|NACL SOLUTION(5,4)\|PROMETHIUM(5,4)\|PULVERIZATION(5,4)\|TRIPLICATE(5,4)\|CENTRIFUGE CELL(5,3)\|BICARBONATE HCO3(5,2)\|AEROSOL SIZED PARTICLE(5,1)\|AGGREGATING GROUND MINERAL(5,1)\|ANALYTICAL LABORATORY(5,1)\|ANCIENT ROCK FORMATION(5,1)\|ANION CONSERVATION(5,1)\|CATEGORY REGULATION(5,1)\|CATION CONSERVATION(5,1)\|CLAUSE XII(5,1)\|DIFFERENCE VROCK VECTOR(5,1)\|DIFFERENCE VSOIL VECTOR(5,1)\|DISSOLVE ALGINATE(5,1)\|DISSOLVED ALGINATE POWDER(5,1)\|DOWNSTREAM ECOSYSTEM(5,1)\|DOWNSTREAM WATERWAY(5,1)\|DTA DH INVERSE(5,1)\|DUST PREVALENCE(5,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)\|FUNGAL ADJUVANT(5,1)\|GROUND MINERAL AGGREGATION(5,1)\|KEY INSIGHT(5,1)\|MICROBIAL CATION EXCHANGER(5,1)\|MINERAL ADJUVANT(5,1)\|MINERAL TON HECTARE(5,1)\|NUTRIENT AVAILABILITY(5,1)\|PELLET DISSOLUTION(5,1)\|PHOSPHATE ZINC PRECIPITATE(5,1)\|PROGRESS FRACTIONATION(5,1)\|QUASI GOVERNMENTAL REGULATOR(5,1)\|RESERVOIR GEOLOGY(5,1)\|SOIL STERILIZATION(5,1)\|SPECIALIZED TOOL(5,1)\|STEAM STERILIZATION(5,1)\|TECHNO ECONOMIC MODELING(5,1)\|ULTIMATE PRICE(5,1)\|UREY REACTION BASIC PREMISE(5,1)\|VERIFICATION VERSION(5,1)\|VERIFIED ENHANCED ROCK(5,1)\|VOLUNTARY MARKET(5,1)\|RARE EARTH ELEMENT(4,18)\|AQUEOUS CO2(4,2)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DISSOLUTION ENHANCING(4,1)\|DIVALENT MG(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|H2CO SUM(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|LB BROTH(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|REACTION THERMODYNAMICS(4,1)\|SECURITIZED CARBON REMOVAL(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|UNSEALING SAMPLE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|XRF ANALYSIS(4,1)\|BAG(3,2)\|CO2 REMOVAL(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|GROWING PLANT(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|SOIL SAMPLE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|CO2 MOLECULAR MASS(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|\|(US20230273174)\|MINERAL AMENDMENT(100,22)\|VERIFICATION(100,18)\|REMOVING CARBON(100,13)\|ENHANCED ROCK(100,8)\|SILICATE MINERAL AGGLOMERATION(66,2)\|COMMINUTED SILICATE MINERAL(57,3)\|ENHANCED ROCK WEATHERING(46,2)\|INTERESTED PARTY(45,1)\|FUNDAMENTAL ISSUE(37,1)\|MINERAL TRANSFORMATION(31,2)\|SAMPLING COLUMN(27,1)\|CARBON MEASUREMENT OBJECTIVE(25,1)\|LANDOWNER(23,1)\|SLOW RELEASE ACIDIFIER(22,3)\|IMMOBILE TRACE ELEMENT(21,25)\|COMMERCIAL ENTERPRISE(17,1)\|GIBBSITE(15,2)\|BINDER(14,3)\|NEODYMIUM(12,11)\|BRUKER PROPRIETARY GEO CALIBRATION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|LANTHANUM(11,9)\|SAMARIUM(11,8)\|SCANDIUM(11,8)\|YTTERBIUM(11,8)\|GADOLINIUM(11,7)\|PRASEODYMIUM(11,6)\|BERYLLIUM(11,2)\|GERMANIUM(11,2)\|RUBIDIUM(11,2)\|ZIRCONIUM(11,2)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|DRAWDOWN CALCULATION(10,4)\|VROCK MONTE CARLO SIMULATION(10,1)\|AVERAGE PARTICLE SIZE(9,4)\|ERW(9,4)\|BLAST FURNACE SLAG(9,2)\|CASO(9,2)\|CESIUM(9,2)\|CHROMIUM(9,2)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|RIGOROUS QUANTIFICATION(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|BIOLOGICAL DERIVED COMPONENT(9,1)\|DIVERSE DECARBONIZATION STRATEGY(9,1)\|PELLETIZED MINERAL AMENDMENT(9,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|GYPSUM(8,3)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|NONLIMITING CANDIDATE(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|STERILIZED SOIL BEAKER(8,1)\|TRANSITION METAL(7,5)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|COMPUTING VROCK(7,2)\|DISSOLUTION KINETICS(7,2)\|PHOSPHATE FERTILIZER(7,2)\|PULVERIZED SILICATE(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|CARBON FLUX(6,3)\|CHARGE IMBALANCE(6,2)\|INORGANIC ADDITIVE(6,2)\|MG PPM DETECTION(6,2)\|NEUTRAL GROUND(6,2)\|ROCK PARTICLE(6,2)\|VROCK DOT PRODUCT(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|AGGREGATED PELLET(6,1)\|AGLIME SUBSTITUTE(6,1)\|AGRICULTURAL SOILS(6,1)\|AGRONOMIC PERFORMANCE EXPECTATION(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|BIOFILM MEDIATING(6,1)\|CO2 REAGENT AVAILABILITY(6,1)\|CO2 UPTAKE(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|DDIC DTA ESTIMATE(6,1)\|FORSTERITE METRIC TON(6,1)\|FORSTERITE TENDENCY(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INFERRED ION FLUX(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|INTENSE SCRUTINY(6,1)\|MARKETING COLLATERAL(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|NONPROFIT ORGANIZATION(6,1)\|OCEAN ACIDIFICATION(6,1)\|PELLET AGGLOMERATION(6,1)\|PHOSPHORUS ECOSYSTEM LOSS(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|PREAPPLICATION SOIL(6,1)\|PROTONATED MICROBE(6,1)\|PULVERIZED LIMESTONE(6,1)\|PULVERIZED MG2SIO(6,1)\|RENOWNED CHEMIST(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|REWET BIOMASS(6,1)\|RIGOROUS COMPLIANCE(6,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)\|SOIL CULTIVATED ZONE(6,1)\|SOIL GEOCHEMISTRY(6,1)\|SOIL HYDROLOGY(6,1)\|NACL SOLUTION(5,4)\|PROMETHIUM(5,4)\|PULVERIZATION(5,4)\|TRIPLICATE(5,4)\|CENTRIFUGE CELL(5,3)\|BICARBONATE HCO3(5,2)\|GROWING PLANT(5,2)\|AEROSOL SIZED PARTICLE(5,1)\|AGGREGATING GROUND MINERAL(5,1)\|ANALYTICAL LABORATORY(5,1)\|ANCIENT ROCK FORMATION(5,1)\|ANION CONSERVATION(5,1)\|CATEGORY REGULATION(5,1)\|CATION CONSERVATION(5,1)\|CLAUSE XII(5,1)\|DIFFERENCE VROCK VECTOR(5,1)\|DIFFERENCE VSOIL VECTOR(5,1)\|DISSOLVE ALGINATE(5,1)\|DISSOLVED ALGINATE POWDER(5,1)\|DOWNSTREAM ECOSYSTEM(5,1)\|DOWNSTREAM WATERWAY(5,1)\|DTA DH INVERSE(5,1)\|DUST PREVALENCE(5,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)\|FUNGAL ADJUVANT(5,1)\|GROUND MINERAL AGGREGATION(5,1)\|KEY INSIGHT(5,1)\|MICROBIAL CATION EXCHANGER(5,1)\|MINERAL ADJUVANT(5,1)\|NUTRIENT AVAILABILITY(5,1)\|PELLET DISSOLUTION(5,1)\|PHOSPHATE ZINC PRECIPITATE(5,1)\|PROGRESS FRACTIONATION(5,1)\|QUASI GOVERNMENTAL REGULATOR(5,1)\|RESERVOIR GEOLOGY(5,1)\|SOIL STERILIZATION(5,1)\|SPECIALIZED TOOL(5,1)\|STEAM STERILIZATION(5,1)\|TECHNO ECONOMIC MODELING(5,1)\|ULTIMATE PRICE(5,1)\|VERIFICATION VERSION(5,1)\|VERIFIED ENHANCED ROCK(5,1)\|VOLUNTARY MARKET(5,1)\|RARE EARTH ELEMENT(4,18)\|AQUEOUS CO2(4,2)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DISSOLUTION ENHANCING(4,1)\|DIVALENT MG(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|H2CO SUM(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|LB BROTH(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|REACTION THERMODYNAMICS(4,1)\|SECURITIZED CARBON REMOVAL(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|UNSEALING SAMPLE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|XRF ANALYSIS(4,1)\|BAG(3,2)\|CO2 REMOVAL(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|SOIL SAMPLE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|CO2 MOLECULAR MASS(2,1)\|COMPACT MASS(2,1)\|\|(US11644454)\|MINERAL AMENDMENT(100,20)\|VERIFICATION(100,18)\|REMOVING CARBON(100,12)\|ENHANCED ROCK(100,8)\|ENHANCED ROCK WEATHERING(100,3)\|INTERESTED PARTY(42,1)\|FUNDAMENTAL ISSUE(35,1)\|IMMOBILE TRACE ELEMENT(33,30)\|SAMPLING COLUMN(26,1)\|CARBON MEASUREMENT OBJECTIVE(24,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(22,1)\|LANDOWNER(22,1)\|SOIL SAMPLE(21,10)\|DIVALENT CATION MEASUREMENT(20,2)\|COMMERCIAL ENTERPRISE(16,1)\|MINERAL AMENDMENT ADDITION(12,1)\|VANADIUM(12,1)\|NEODYMIUM(11,11)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|PRASEODYMIUM(11,6)\|BRUKER PROPRIETARY GEO CALIBRATION(11,1)\|LANTHANUM(10,9)\|SAMARIUM(10,8)\|SCANDIUM(10,8)\|YTTERBIUM(10,8)\|GADOLINIUM(10,7)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|BERYLLIUM(10,2)\|GERMANIUM(10,2)\|RUBIDIUM(10,2)\|ZIRCONIUM(10,2)\|DRAWDOWN CALCULATION(9,4)\|ERW(9,4)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|VROCK MONTE CARLO SIMULATION(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|CESIUM(8,2)\|CHROMIUM(8,2)\|NONLIMITING CANDIDATE(8,2)\|RIGOROUS QUANTIFICATION(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|DIVERSE DECARBONIZATION STRATEGY(8,1)\|PELLETIZED MINERAL AMENDMENT(8,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(8,1)\|STERILIZED SOIL BEAKER(8,1)\|ETHYLENEDIAMINETETRAACETIC ACID(7,4)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|PHOSPHATE FERTILIZER(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|TRANSITION METAL(6,5)\|CARBON FLUX(6,3)\|APPLIED DIVALENT CATION(6,2)\|COMPUTING VROCK(6,2)\|DISSOLUTION KINETICS(6,2)\|PULVERIZED SILICATE(6,2)\|ROCK PARTICLE(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|CO2 REAGENT AVAILABILITY(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|FORSTERITE METRIC TON(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|PELLET AGGLOMERATION(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|CENTRIFUGE CELL(5,3)\|BICARBONATE HCO3(5,2)\|CHARGE IMBALANCE(5,2)\|GROWING PLANT(5,2)\|INORGANIC ADDITIVE(5,2)\|MG PPM DETECTION(5,2)\|NEUTRAL GROUND(5,2)\|VROCK DOT PRODUCT(5,2)\|AGGREGATED PELLET(5,1)\|AGLIME SUBSTITUTE(5,1)\|AGRICULTURAL SOILS(5,1)\|AGRONOMIC PERFORMANCE EXPECTATION(5,1)\|BIOFILM MEDIATING(5,1)\|CO2 UPTAKE(5,1)\|DDIC DTA ESTIMATE(5,1)\|FORSTERITE TENDENCY(5,1)\|INFERRED ION FLUX(5,1)\|INTENSE SCRUTINY(5,1)\|MARKETING COLLATERAL(5,1)\|NONPROFIT ORGANIZATION(5,1)\|OCEAN ACIDIFICATION(5,1)\|PHOSPHORUS ECOSYSTEM LOSS(5,1)\|PREAPPLICATION SOIL(5,1)\|PROTONATED MICROBE(5,1)\|PULVERIZED LIMESTONE(5,1)\|PULVERIZED MG2SIO(5,1)\|RENOWNED CHEMIST(5,1)\|REWET BIOMASS(5,1)\|RIGOROUS COMPLIANCE(5,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(5,1)\|SOIL CULTIVATED ZONE(5,1)\|SOIL GEOCHEMISTRY(5,1)\|SOIL HYDROLOGY(5,1)\|X RAY FLUORESCENCE SPECTROSCOPY(5,1)\|RARE EARTH ELEMENT(4,18)\|NACL SOLUTION(4,4)\|PROMETHIUM(4,4)\|PULVERIZATION(4,4)\|TRIPLICATE(4,4)\|AQUEOUS CO2(4,2)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AEROSOL SIZED PARTICLE(4,1)\|AGGREGATING GROUND MINERAL(4,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)\|ANALYTICAL LABORATORY(4,1)\|ANCIENT ROCK FORMATION(4,1)\|ANION CONSERVATION(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|CATEGORY REGULATION(4,1)\|CATION CONSERVATION(4,1)\|CLAUSE XII(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DIFFERENCE VROCK VECTOR(4,1)\|DIFFERENCE VSOIL VECTOR(4,1)\|DISSOLUTION ENHANCING(4,1)\|DISSOLVE ALGINATE(4,1)\|DISSOLVED ALGINATE POWDER(4,1)\|DIVALENT MG(4,1)\|DOWNSTREAM ECOSYSTEM(4,1)\|DOWNSTREAM WATERWAY(4,1)\|DTA DH INVERSE(4,1)\|DUST PREVALENCE(4,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|FUNGAL ADJUVANT(4,1)\|GROUND MINERAL AGGREGATION(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|H2CO SUM(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|KEY INSIGHT(4,1)\|LB BROTH(4,1)\|MICROBIAL CATION EXCHANGER(4,1)\|MINERAL ADJUVANT(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|NUTRIENT AVAILABILITY(4,1)\|PELLET DISSOLUTION(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|PROGRESS FRACTIONATION(4,1)\|QUASI GOVERNMENTAL REGULATOR(4,1)\|REACTION THERMODYNAMICS(4,1)\|RESERVOIR GEOLOGY(4,1)\|SECURITIZED CARBON REMOVAL(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|SOIL STERILIZATION(4,1)\|SPECIALIZED TOOL(4,1)\|STEAM STERILIZATION(4,1)\|TECHNO ECONOMIC MODELING(4,1)\|ULTIMATE PRICE(4,1)\|UNSEALING SAMPLE(4,1)\|UREY REACTION BASIC PREMISE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|VERIFICATION VERSION(4,1)\|VERIFIED ENHANCED ROCK(4,1)\|VOLUNTARY MARKET(4,1)\|XRF ANALYSIS(4,1)\|CARBON DIOXIDE REMOVAL(3,10)\|BAG(3,2)\|BINDER(3,2)\|CO2 REMOVAL(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PHOSPHATE ZINC PRECIPITATE(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SLOW RELEASE ACIDIFIER(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|4H4SIO(2,1)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|CO2 MOLECULAR MASS(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|\|(US20220404329)\|MINERAL AMENDMENT(100,30)\|VERIFICATION(100,17)\|REMOVING CARBON(100,13)\|ENHANCED ROCK(100,8)\|ENHANCED ROCK WEATHERING(100,3)\|SILICATE MINERAL AGGLOMERATION(46,2)\|COMMINUTED SILICATE MINERAL(39,3)\|IMMOBILE TRACE ELEMENT(32,34)\|INTERESTED PARTY(31,1)\|FUNDAMENTAL ISSUE(25,1)\|MINERAL TRANSFORMATION(21,2)\|ETHYLENE DIAMINE TETRAACETIC ACID(20,1)\|SAMPLING COLUMN(19,1)\|CARBON MEASUREMENT OBJECTIVE(18,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(16,1)\|LANDOWNER(16,1)\|SOIL SAMPLE(15,10)\|SLOW RELEASE ACIDIFIER(15,3)\|DIVALENT CATION MEASUREMENT(15,2)\|BERYLLIUM(12,3)\|VANADIUM(12,2)\|COMMERCIAL ENTERPRISE(12,1)\|DYSPROSIUM(11,10)\|GADOLINIUM(11,8)\|PRASEODYMIUM(11,7)\|GERMANIUM(11,3)\|RUBIDIUM(11,3)\|ZIRCONIUM(11,3)\|NEODYMIUM(10,12)\|EUROPIUM(10,11)\|LANTHANUM(10,10)\|SAMARIUM(10,9)\|SCANDIUM(10,9)\|YTTERBIUM(10,9)\|HOLMIUM(10,7)\|LUTETIUM(10,7)\|THULIUM(10,7)\|BINDER(10,3)\|GALLIUM(10,3)\|HAFNIUM(10,3)\|NIOBIUM(10,3)\|TANTALUM(10,3)\|GIBBSITE(10,2)\|RARE METAL(9,6)\|CESIUM(9,3)\|CHROMIUM(9,3)\|MINERAL AMENDMENT ADDITION(9,1)\|CERIUM(8,10)\|YTTRIUM(8,9)\|BRUKER PROPRIETARY GEO CALIBRATION(8,1)\|TRANSITION METAL(7,7)\|DRAWDOWN CALCULATION(7,4)\|VROCK MONTE CARLO SIMULATION(7,1)\|AVERAGE PARTICLE SIZE(6,4)\|ERW(6,4)\|GYPSUM(6,3)\|BLAST FURNACE SLAG(6,2)\|CASO(6,2)\|RIGOROUS QUANTIFICATION(6,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(6,2)\|BIOLOGICAL DERIVED COMPONENT(6,1)\|DELIVER PROSPECTIVE REWARD(6,1)\|DIVERSE DECARBONIZATION STRATEGY(6,1)\|PELLETIZED MINERAL AMENDMENT(6,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(6,1)\|STERILIZED SOIL BEAKER(6,1)\|RARE EARTH ELEMENT(5,20)\|PPB DETECTION(5,4)\|INSTRUMENTAL ERROR(5,3)\|MINERAL SOIL AMENDMENT(5,3)\|AIRTIGHT CONTAINMENT(5,2)\|APPLIED DIVALENT CATION(5,2)\|COMPUTING VROCK(5,2)\|DISSOLUTION KINETICS(5,2)\|NONLIMITING CANDIDATE(5,2)\|PHOSPHATE FERTILIZER(5,2)\|PULVERIZED SILICATE(5,2)\|ALKALIZER KINETICS(5,1)\|MINERAL ADDITIVE PROVEN IDENTITY(5,1)\|SOIL ORGANIC CARBON(5,1)\|TAXONOMY DISTINGUISHE(5,1)\|UNINHABITABLE WATERWAY(5,1)\|WET BIOMASS WET ALIQUOT(5,1)\|CARBON FLUX(4,3)\|CENTRIFUGE CELL(4,3)\|CHARGE IMBALANCE(4,2)\|INORGANIC ADDITIVE(4,2)\|MG PPM DETECTION(4,2)\|NEUTRAL GROUND(4,2)\|ROCK PARTICLE(4,2)\|VROCK DOT PRODUCT(4,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(4,1)\|AGGREGATED PELLET(4,1)\|AGLIME SUBSTITUTE(4,1)\|AGRICULTURAL SOILS(4,1)\|AGRONOMIC PERFORMANCE EXPECTATION(4,1)\|ALKALINITY EXPORT(4,1)\|BIODEGRADABLE TRANSPORTER(4,1)\|BIOFILM MEDIATING(4,1)\|CO2 REAGENT AVAILABILITY(4,1)\|CO2 UPTAKE(4,1)\|CUMULATIVE CATION FLUX MEASURE(4,1)\|DDIC DTA ESTIMATE(4,1)\|FORSTERITE METRIC TON(4,1)\|FORSTERITE TENDENCY(4,1)\|HENRY LAW COEFFICIENT(4,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(4,1)\|INFERRED ION FLUX(4,1)\|INSTRUMENTAL UNCERTAINTY(4,1)\|INTENSE SCRUTINY(4,1)\|MARKETING COLLATERAL(4,1)\|MICRONUTRIENT INCORPORATION(4,1)\|MYCORRHIZAL INOCULUM(4,1)\|NONPROFIT ORGANIZATION(4,1)\|OCEAN ACIDIFICATION(4,1)\|PELLET AGGLOMERATION(4,1)\|PHOSPHORUS ECOSYSTEM LOSS(4,1)\|PORTABLE XRF INSTRUMENT(4,1)\|PREAPPLICATION SOIL(4,1)\|PROTONATED MICROBE(4,1)\|PULVERIZED LIMESTONE(4,1)\|PULVERIZED MG2SIO(4,1)\|RENOWNED CHEMIST(4,1)\|RESPIRATORY HEALTH IMPACT(4,1)\|REWET BIOMASS(4,1)\|RIGOROUS COMPLIANCE(4,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(4,1)\|SOIL CULTIVATED ZONE(4,1)\|SOIL GEOCHEMISTRY(4,1)\|SOIL HYDROLOGY(4,1)\|X RAY FLUORESCENCE SPECTROSCOPY(4,1)\|CARBON DIOXIDE REMOVAL(3,9)\|NACL SOLUTION(3,4)\|PROMETHIUM(3,4)\|PULVERIZATION(3,4)\|TRIPLICATE(3,4)\|AQUEOUS CO2(3,2)\|AVOIDED EMISSION(3,2)\|BICARBONATE HCO3(3,2)\|CARBONATE SPECIES(3,2)\|DISSOLVED CARBONATE(3,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(3,2)\|GROWING PLANT(3,2)\|MINERAL POTENTIAL(3,2)\|SECURE VESSEL(3,2)\|SOIL ENVIRONMENT(3,2)\|ABUNDANT CO2(3,1)\|ACCELERATE TIMING(3,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(3,1)\|AEROSOL SIZED PARTICLE(3,1)\|AGGREGATING GROUND MINERAL(3,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(3,1)\|ANALYTICAL LABORATORY(3,1)\|ANCIENT ROCK FORMATION(3,1)\|ANION CONSERVATION(3,1)\|AQUEOUS BICARBONATE MEASUREMENT(3,1)\|AQUEOUS COMPLEXATION(3,1)\|ASBESTOS EXPOSURE(3,1)\|ASSEMBLING MP(3,1)\|ATTENDANT DEMAND(3,1)\|AUXILIARY GEOCHEMICAL DATA(3,1)\|BICARBONATE MOLE(3,1)\|BROAD FRAMEWORK(3,1)\|CARBON EXCHANGE TRANSACTION(3,1)\|CARBON VERIFICATION BENEFIT(3,1)\|CATEGORY REGULATION(3,1)\|CATION CONSERVATION(3,1)\|CLAUSE XII(3,1)\|COARSE PARTICLE(3,1)\|COLLECT CELL PELLET(3,1)\|CONTINENTAL COLLISION RELEASE(3,1)\|CROP HEALTH(3,1)\|DIFFERENCE VROCK VECTOR(3,1)\|DIFFERENCE VSOIL VECTOR(3,1)\|DISSOLUTION ENHANCING(3,1)\|DISSOLVE ALGINATE(3,1)\|DISSOLVED ALGINATE POWDER(3,1)\|DIVALENT MG(3,1)\|DOWNSTREAM ECOSYSTEM(3,1)\|DOWNSTREAM WATERWAY(3,1)\|DTA DH INVERSE(3,1)\|DUST PREVALENCE(3,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(3,1)\|EQUILIBRIUM EQUATION(3,1)\|FERTILIZATION FREQUENCY(3,1)\|FRAUDULENT SAMPLE(3,1)\|FUNGAL ADJUVANT(3,1)\|GROUND MINERAL AGGREGATION(3,1)\|GROUND NATURAL ENVIRONMENT(3,1)\|H2CO SUM(3,1)\|INCREASE ECOSYSTEM COBENEFIT(3,1)\|KEY INSIGHT(3,1)\|LB BROTH(3,1)\|MICROBIAL CATION EXCHANGER(3,1)\|MINERAL ADJUVANT(3,1)\|MINERAL TRANSFORMATION EXTENT(3,1)\|MINUS PROTON DONOR(3,1)\|NUTRIENT AVAILABILITY(3,1)\|PELLET DISSOLUTION(3,1)\|PHOSPHATE LEACHING(3,1)\|PHOSPHATE MOBILITY(3,1)\|PRECISE ANSWER(3,1)\|PREEQUILIBRATED TUBE(3,1)\|PROGRESS FRACTIONATION(3,1)\|QUASI GOVERNMENTAL REGULATOR(3,1)\|REACTION THERMODYNAMICS(3,1)\|RESERVOIR GEOLOGY(3,1)\|SECURITIZED CARBON REMOVAL(3,1)\|SILICATE MINERAL SHELL(3,1)\|SILICATE ROLE(3,1)\|SOIL STERILIZATION(3,1)\|SPECIALIZED TOOL(3,1)\|STEAM STERILIZATION(3,1)\|TECHNO ECONOMIC MODELING(3,1)\|ULTIMATE PRICE(3,1)\|UNSEALING SAMPLE(3,1)\|UREY REACTION BASIC PREMISE(3,1)\|VERIFIABLE CARBON REMOVAL(3,1)\|VERIFICATION VERSION(3,1)\|VERIFIED ENHANCED ROCK(3,1)\|VOLUNTARY MARKET(3,1)\|XRF ANALYSIS(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|BAG(2,2)\|CO2 REMOVAL(2,2)\|COMMINUTION(2,2)\|FARMER(2,2)\|MARKET ABILITY(2,2)\|PELLETIZING(2,2)\|PRODUCT FORMULATION(2,2)\|STAKEHOLDER(2,2)\|TOTAL FORMULATION(2,2)\|ACIDIC ENVIRONMENT(2,1)\|ANALYTICAL PERFORMANCE(2,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(2,1)\|CARBON MARKET MATURATION(2,1)\|CARBON REMOVAL VERIFICATION(2,1)\|CARBON TRANSACTION(2,1)\|COMPUTING INDEX(2,1)\|CORTEVA CARBON(2,1)\|DRIED PELLET(2,1)\|EMPLACEMENT LOCATION(2,1)\|ENTIRE US ECONOMY(2,1)\|EXCHANGE COEFFICIENT(2,1)\|EXCHANGING RESIN(2,1)\|EXPERIMENTAL WORK(2,1)\|EXTANT FARM EQUIPMENT(2,1)\|FILTRATE ANALYSIS(2,1)\|FULL SUMMATION(2,1)\|GRIND CELL(2,1)\|HEAVY PHOSPHATE(2,1)\|ICP ANALYSIS(2,1)\|IMMOBILIZATION(2,1)\|INDIGO CARBON(2,1)\|LABORATORY SETTING(2,1)\|MARINE SETTING(2,1)\|MINERAL DELIVERY(2,1)\|MINERAL DISSOLUTION RATE(2,1)\|NATURAL ABUNDANCE CALCULATION(2,1)\|NATURAL SOILS(2,1)\|NEGATIVE EMISSION(2,1)\|PHOSPHATE ZINC PRECIPITATE(2,1)\|PLANT DEMAND(2,1)\|PROJECT EVALUATION CRITERIA(2,1)\|RELEVANT ION(2,1)\|ROCK ELEMENTAL ANALYSIS(2,1)\|ROCK MATERIAL ACCELERATED WEATHERING(2,1)\|SAMPLING DENSITY(2,1)\|SHARP THRESHOLD(2,1)\|SOIL ELEMENTAL ANALYSIS(2,1)\|SUBSURFACE SOIL PORE WATER(2,1)\|TECHNOLOGICAL SOLUTION(2,1)\|WET GRAM(2,1)\|ABILITY THRESHOLD(1,1)\|ACCEPTANCE(1,1)\|ACCOUNTING(1,1)\|ACID TREATED ARTHROBACTER(1,1)\|ACIDIC SOIL SOLUTION(1,1)\|ADDITIONALITY(1,1)\|ADMIXTURE(1,1)\|AERATION(1,1)\|AGLIME MESH SIZE OBSERVATION(1,1)\|AGRICULTURE(1,1)\|ALGAL BLOOM(1,1)\|ANALYTICAL SOLUTION(1,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(1,1)\|ATTRACTION(1,1)\|AUTOCLAVE(1,1)\|BACTERIA(1,1)\|BIOADSORBED METAL ACTIVE RELEASE(1,1)\|BIOFUEL(1,1)\|CA BEARING SILICATE(1,1)\|CA CONTENT(1,1)\|CALIBRATION STANDARD(1,1)\|CAPTURING CARBON(1,1)\|CATION EXCHANGE COLUMN(1,1)\|CHARGE BALANCE(1,1)\|CHELATOR(1,1)\|CHITOSAN(1,1)\|CLASSIFICATION(1,1)\|CLAWBACK(1,1)\|CLIMEWORK(1,1)\|\|(US20260016458)\|MINERAL AMENDMENT(100,20)\|VERIFICATION(100,17)\|REMOVING CARBON(100,12)\|ENHANCED ROCK(100,7)\|VERIFYING ENHANCED ROCK WEATHERING(70,1)\|IMMOBILE TRACE ELEMENT(55,11)\|ENHANCED ROCK WEATHERING(43,2)\|INTERESTED PARTY(42,1)\|RECOVERING SAMPLING COLUMN(36,1)\|FUNDAMENTAL ISSUE(35,1)\|CARBON MEASUREMENT OBJECTIVE(24,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(22,1)\|LANDOWNER(22,1)\|SOIL SAMPLE(21,10)\|DIVALENT CATION MEASUREMENT(20,2)\|COMMERCIAL ENTERPRISE(16,1)\|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)\|MINERAL AMENDMENT ADDITION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|PRASEODYMIUM(11,6)\|BRUKER PROPRIETARY GEO CALIBRATION(11,1)\|LANTHANUM(10,9)\|SAMARIUM(10,8)\|SCANDIUM(10,8)\|YTTERBIUM(10,8)\|GADOLINIUM(10,7)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|BERYLLIUM(10,2)\|GERMANIUM(10,2)\|RUBIDIUM(10,2)\|SIO PERCENT MINERALOGICAL FRACTION(10,2)\|ZIRCONIUM(10,2)\|DRAWDOWN CALCULATION(9,4)\|ERW(9,4)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|REES PPB DETECTION(9,2)\|TANTALUM(9,2)\|ANDTHE TRANSITION METAL(9,1)\|DAC PROJECT RIGOROUS QUANTIFICATION(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE EARTH ELEMENT(8,6)\|RARE METAL(8,4)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|CESIUM(8,2)\|CHROMIUM(8,2)\|ETHYLENEDIAMINETETRAACETIC ACID(8,2)\|NONLIMITING CANDIDATE(8,2)\|REE TRIPLICATE(8,2)\|CARBON DIOXIDE REMOVAL FRACTIONATION(8,1)\|DELIVER PROSPECTIVE REWARD(8,1)\|PELLETIZED MINERAL AMENDMENT(8,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(8,1)\|STERILIZED SOIL BEAKER(8,1)\|INSTRUMENTAL ERROR(7,3)\|PHOSPHATE FERTILIZER(7,2)\|ALKALIZER KINETICS(7,1)\|DAC ULTIMATE PRICE(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|PHOSPHATE LEACHING LIKELIHOOD(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|TRANSITION METAL(6,5)\|CARBON FLUX(6,3)\|APPLIED DIVALENT CATION(6,2)\|CDR CALCULATION(6,2)\|DISSOLUTION KINETICS(6,2)\|PULVERIZED SILICATE(6,2)\|ROCK PARTICLE(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|FORSTERITE METRIC TON(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|ITE FINGERPRINT(6,1)\|ITES ABUNDANCE(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|PELLET AGGLOMERATION(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|CENTRIFUGE CELL(5,3)\|CHARGE IMBALANCE(5,2)\|GROWING PLANT(5,2)\|INORGANIC ADDITIVE(5,2)\|MG PPM DETECTION(5,2)\|NEUTRAL GROUND(5,2)\|AGGREGATED PELLET(5,1)\|AGLIME SUBSTITUTE(5,1)\|AGRICULTURAL SOILS(5,1)\|AGRONOMIC PERFORMANCE EXPECTATION(5,1)\|BIOFILM MEDIATING(5,1)\|DDIC DTA ESTIMATE(5,1)\|DRAWDOWN ESTIMATION(5,1)\|FORSTERITE TENDENCY(5,1)\|INFERRED ION FLUX(5,1)\|INTENSE SCRUTINY(5,1)\|ITES PROPORTION(5,1)\|MARKETING COLLATERAL(5,1)\|NEGATIVELY CHARGED BICARBONATE(5,1)\|NONPROFIT ORGANIZATION(5,1)\|OCEAN ACIDIFICATION(5,1)\|PHOSPHORUS ECOSYSTEM LOSS(5,1)\|PREAPPLICATION SOIL(5,1)\|PROTONATED MICROBE(5,1)\|PULVERIZED LIMESTONE(5,1)\|RENOWNED CHEMIST(5,1)\|REWET BIOMASS(5,1)\|RIGOROUS COMPLIANCE(5,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(5,1)\|SOIL CULTIVATED ZONE(5,1)\|SOIL GEOCHEMISTRY(5,1)\|SOIL HYDROLOGY(5,1)\|X RAY FLUORESCENCE SPECTROSCOPY(5,1)\|NACL SOLUTION(4,4)\|PROMETHIUM(4,4)\|PULVERIZATION(4,4)\|AVOIDED EMISSION(4,2)\|CARBONATE DISSOLUTION(4,2)\|CARBONATE SPECIES(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AEROSOL SIZED PARTICLE(4,1)\|AGGREGATING GROUND MINERAL(4,1)\|ANALYTICAL LABORATORY(4,1)\|ANCIENT ROCK FORMATION(4,1)\|ANION CONSERVATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|CATEGORY REGULATION(4,1)\|CATION CONSERVATION(4,1)\|CLAUSE XII(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|CUSTOM ITE STANDARD(4,1)\|DISSOLUTION ENHANCING(4,1)\|DISSOLVE ALGINATE(4,1)\|DISSOLVED ALGINATE(4,1)\|DIVALENT MG(4,1)\|DOWNSTREAM ECOSYSTEM(4,1)\|DOWNSTREAM WATERWAY(4,1)\|DTA DH INVERSE(4,1)\|DUST PREVALENCE(4,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|FUNGAL ADJUVANT(4,1)\|GROUND MINERAL AGGREGATION(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|HEAVY PHOSPHATE(4,1)\|HEAVY REES(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|KEY INSIGHT(4,1)\|LB BROTH(4,1)\|MICROBIAL CATION EXCHANGER(4,1)\|MINERAL ADJUVANT(4,1)\|MINERAL TON HECTARE(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|NATIVE ITE(4,1)\|NUTRIENT AVAILABILITY(4,1)\|PELLET DISSOLUTION(4,1)\|PHOSPHATE MOBILITY(4,1)\|PPM NEODYMIUM(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|PROGRESS FRACTIONATION(4,1)\|PULVERIZED MG(4,1)\|QUASI GOVERNMENTAL REGULATOR(4,1)\|REACTION THERMODYNAMICS(4,1)\|REE AQUEOUS COMPLEXATION(4,1)\|REES FULL RECOVERY(4,1)\|RESERVOIR GEOLOGY(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|SOIL STERILIZATION(4,1)\|SPECIALIZED TOOL(4,1)\|STEAM STERILIZATION(4,1)\|TECHNICAL CDR(4,1)\|TECHNO ECONOMIC MODELING(4,1)\|UNSEALING SAMPLE(4,1)\|UREY REACTION BASIC PREMISE(4,1)\|V MONTE CARLO SIMULATION(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|VERIFICATION VERSION(4,1)\|VERIFIED ENHANCED ROCK(4,1)\|VOLUNTARY MARKET(4,1)\|XRF ANALYSIS(4,1)\|HCO(3,4)\|K2H(3,4)\|BAG(3,2)\|BINDER(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|AQUEOUS BICARBONATE(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|ITES COST(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PHOSPHATE ZINC PRECIPITATE(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SLOW RELEASE ACIDIFIER(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|K1H(2,3)\|LYSE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|\|(WO2022/271842)\|MINERAL AMENDMENT(100,30)\|VERIFICATION(100,19)\|REMOVING CARBON(100,14)\|ENHANCED ROCK(100,10)\|ENHANCED ROCK WEATHERING(100,3)\|SILICATE MINERAL AGGLOMERATION(46,2)\|COMMINUTED SILICATE MINERAL(39,3)\|IMMOBILE TRACE ELEMENT(32,34)\|INTERESTED PARTY(31,1)\|FUNDAMENTAL ISSUE(25,1)\|SAMPLING COLUMN(19,1)\|CARBON MEASUREMENT OBJECTIVE(18,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(16,1)\|LANDOWNER(16,1)\|SOIL SAMPLE(15,10)\|SLOW RELEASE ACIDIFIER(15,3)\|DIVALENT CATION MEASUREMENT(15,2)\|BERYLLIUM(12,3)\|VANADIUM(12,2)\|COMMERCIAL ENTERPRISE(12,1)\|DYSPROSIUM(11,10)\|GADOLINIUM(11,8)\|PRASEODYMIUM(11,7)\|GERMANIUM(11,3)\|RUBIDIUM(11,3)\|ZIRCONIUM(11,3)\|NEODYMIUM(10,12)\|EUROPIUM(10,11)\|LANTHANUM(10,10)\|SAMARIUM(10,9)\|SCANDIUM(10,9)\|YTTERBIUM(10,9)\|HOLMIUM(10,7)\|LUTETIUM(10,7)\|THULIUM(10,7)\|BINDER(10,3)\|GALLIUM(10,3)\|HAFNIUM(10,3)\|NIOBIUM(10,3)\|TANTALUM(10,3)\|GIBBSITE(10,2)\|RARE METAL(9,6)\|CESIUM(9,3)\|CHROMIUM(9,3)\|MINERAL AMENDMENT ADDITION(9,1)\|CERIUM(8,10)\|YTTRIUM(8,9)\|BRUKER PROPRIETARY GEO CALIBRATION(8,1)\|TRANSITION METAL(7,7)\|DRAWDOWN CALCULATION(7,4)\|ETHYLENEDIAMINETETRAACETIC ACID(7,1)\|VR0CK MONTE CARLO SIMULATION(7,1)\|AVERAGE PARTICLE SIZE(6,4)\|ERW(6,4)\|GYPSUM(6,3)\|MINERAL SOIL AMENDMENT(6,3)\|BLAST FURNACE SLAG(6,2)\|RIGOROUS QUANTIFICATION(6,2)\|BIOLOGICAL DERIVED COMPONENT(6,1)\|DDIC DH DTA(6,1)\|DELIVER PROSPECTIVE REWARD(6,1)\|DIVERSE DECARBONIZATION STRATEGY(6,1)\|PELLETIZED MINERAL AMENDMENT(6,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(6,1)\|STERILIZED SOIL BEAKER(6,1)\|RARE EARTH ELEMENT(5,20)\|PPB DETECTION(5,4)\|INSTRUMENTAL ERROR(5,3)\|AIRTIGHT CONTAINMENT(5,2)\|APPLIED DIVALENT CATION(5,2)\|COMPUTING VROCK(5,2)\|DISSOLUTION KINETICS(5,2)\|NONLIMITING CANDIDATE(5,2)\|PHOSPHATE FERTILIZER(5,2)\|PULVERIZED SILICATE(5,2)\|SI PERCENT MINERALOGICAL FRACTION(5,2)\|ALKALIZER KINETICS(5,1)\|MINERAL ADDITIVE PROVEN IDENTITY(5,1)\|SOIL ORGANIC CARBON(5,1)\|TAXONOMY DISTINGUISHE(5,1)\|UNINHABITABLE WATERWAY(5,1)\|WET BIOMASS WET ALIQUOT(5,1)\|CARBON FLUX(4,3)\|CENTRIFUGE CELL(4,3)\|CHARGE IMBALANCE(4,2)\|INORGANIC ADDITIVE(4,2)\|MG PPM DETECTION(4,2)\|NEUTRAL GROUND(4,2)\|ROCK PARTICLE(4,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(4,1)\|AGGREGATED PELLET(4,1)\|AGLIME SUBSTITUTE(4,1)\|AGRICULTURAL SOILS(4,1)\|AGRONOMIC PERFORMANCE EXPECTATION(4,1)\|ALKALINITY EXPORT(4,1)\|BIODEGRADABLE TRANSPORTER(4,1)\|BIOFILM MEDIATING(4,1)\|CO2 REAGENT AVAILABILITY(4,1)\|CO2 UPTAKE(4,1)\|CUMULATIVE CATION FLUX MEASURE(4,1)\|DDIC DTA ESTIMATE(4,1)\|DRAWDOWN ESTIMATION(4,1)\|FORSTERITE METRIC TON(4,1)\|FORSTERITE TENDENCY(4,1)\|HENRY LAW COEFFICIENT(4,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(4,1)\|INFERRED ION FLUX(4,1)\|INSTRUMENTAL UNCERTAINTY(4,1)\|INTENSE SCRUTINY(4,1)\|MARKETING COLLATERAL(4,1)\|MICRONUTRIENT INCORPORATION(4,1)\|MYCORRHIZAL INOCULUM(4,1)\|NEGATIVELY CHARGED BICARBONATE(4,1)\|NONPROFIT ORGANIZATION(4,1)\|OCEAN ACIDIFICATION(4,1)\|PELLET AGGLOMERATION(4,1)\|PHOSPHORUS ECOSYSTEM LOSS(4,1)\|PORTABLE XRF INSTRUMENT(4,1)\|PREAPPLICATION SOIL(4,1)\|PROTONATED MICROBE(4,1)\|PULVERIZED LIMESTONE(4,1)\|PULVERIZED MGISICE(4,1)\|RENOWNED CHEMIST(4,1)\|RESPIRATORY HEALTH IMPACT(4,1)\|REWET BIOMASS(4,1)\|RIGOROUS COMPLIANCE(4,1)\|RLE TRIPLICATE(4,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(4,1)\|SOIL CULTIVATED ZONE(4,1)\|SOIL GEOCHEMISTRY(4,1)\|SOIL HYDROLOGY(4,1)\|X RAY FLUORESCENCE SPECTROSCOPY(4,1)\|CARBON DIOXIDE REMOVAL(3,9)\|NACL SOLUTION(3,4)\|PROMETHIUM(3,4)\|PULVERIZATION(3,4)\|AQUEOUS CO2(3,2)\|AVOIDED EMISSION(3,2)\|CARBONATE SPECIES(3,2)\|DISSOLVED CARBONATE(3,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(3,2)\|GROWING PLANT(3,2)\|MINERAL POTENTIAL(3,2)\|SECURE VESSEL(3,2)\|SOIL ENVIRONMENT(3,2)\|ACCELERATE TIMING(3,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(3,1)\|AEROSOL SIZED PARTICLE(3,1)\|AGGREGATING GROUND MINERAL(3,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(3,1)\|ANALYTICAL LABORATORY(3,1)\|ANCIENT ROCK FORMATION(3,1)\|ANION CONSERVATION(3,1)\|AQUEOUS BICARBONATE MEASUREMENT(3,1)\|AQUEOUS COMPLEXATION(3,1)\|ASBESTOS EXPOSURE(3,1)\|ASSEMBLING MP(3,1)\|ATTENDANT DEMAND(3,1)\|AUXILIARY GEOCHEMICAL DATA(3,1)\|BICARBONATE MOLE(3,1)\|BROAD FRAMEWORK(3,1)\|CARBON EXCHANGE TRANSACTION(3,1)\|CARBON VERIFICATION BENEFIT(3,1)\|CATEGORY REGULATION(3,1)\|CATION CONSERVATION(3,1)\|CLAUSE XII(3,1)\|COARSE PARTICLE(3,1)\|CONTINENTAL COLLISION RELEASE(3,1)\|CROP HEALTH(3,1)\|DIFFERENCE VR0CK VECTOR(3,1)\|DIFFERENCE VSOU VECTOR(3,1)\|DISSOLUTION ENHANCING(3,1)\|DISSOLVE ALGINATE(3,1)\|DISSOLVED ALGINATE POWDER(3,1)\|DIVALENT MG(3,1)\|DOWNSTREAM ECOSYSTEM(3,1)\|DOWNSTREAM WATERWAY(3,1)\|DTA DH INVERSE(3,1)\|DUST PREVALENCE(3,1)\|ECOSYSTEM CO BENEFIT(3,1)\|EQUILIBRIUM EQUATION(3,1)\|FERTILIZATION FREQUENCY(3,1)\|FRAUDULENT SAMPLE(3,1)\|FUNGAL ADJUVANT(3,1)\|GROUND MINERAL AGGREGATION(3,1)\|GROUND NATURAL ENVIRONMENT(3,1)\|H2CO SUM(3,1)\|INCREASE ECOSYSTEM COBENEFIT(3,1)\|KEY INSIGHT(3,1)\|LB BROTH(3,1)\|MICROBIAL CATION EXCHANGER(3,1)\|MINERAL ADJUVANT(3,1)\|MINERAL TRANSFORMATION EXTENT(3,1)\|MINUS PROTON DONOR(3,1)\|NUTRIENT AVAILABILITY(3,1)\|PELLET DISSOLUTION(3,1)\|PHOSPHATE LEACHING(3,1)\|PHOSPHATE MOBILITY(3,1)\|PRECISE ANSWER(3,1)\|PREEQUILIBRATED TUBE(3,1)\|PROGRESS FRACTIONATION(3,1)\|QUASI GOVERNMENTAL REGULATOR(3,1)\|REACTION THERMODYNAMICS(3,1)\|RESERVOIR GEOLOGY(3,1)\|SECURITIZED CARBON REMOVAL(3,1)\|SILICATE MINERAL SHELL(3,1)\|SILICATE ROLE(3,1)\|SOIL STERILIZATION(3,1)\|SPECIALIZED TOOL(3,1)\|STEAM STERILIZATION(3,1)\|STYRENE DIVINYLBENZENE(3,1)\|TECHNO ECONOMIC MODELING(3,1)\|TREATMENT UNIFORMITY(3,1)\|ULTIMATE PRICE(3,1)\|UNSEALING SAMPLE(3,1)\|UREY REACTION BASIC PREMISE(3,1)\|VERIFIABLE CARBON REMOVAL(3,1)\|VERIFICATION VERSION(3,1)\|VERIFIED ENHANCED ROCK(3,1)\|VOLUNTARY MARKET(3,1)\|VROCK DOT PRODUCT(3,1)\|XRF ANALYSIS(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|BAG(2,2)\|CO2 REMOVAL(2,2)\|FARMER(2,2)\|MARKET ABILITY(2,2)\|PELLETIZING(2,2)\|PRODUCT FORMULATION(2,2)\|STAKEHOLDER(2,2)\|TOTAL FORMULATION(2,2)\|ACIDIC ENVIRONMENT(2,1)\|ANALYTICAL PERFORMANCE(2,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(2,1)\|CARBON MARKET MATURATION(2,1)\|CARBON REMOVAL VERIFICATION(2,1)\|CARBON TRANSACTION(2,1)\|CELL PELLET(2,1)\|COMPUTING INDEX(2,1)\|CORTEVA CARBON(2,1)\|DRIED PELLET(2,1)\|EMPLACEMENT LOCATION(2,1)\|ENHANCED ROCK VARIABLE PERFORMANCE(2,1)\|ENTIRE US ECONOMY(2,1)\|EXCHANGE COEFFICIENT(2,1)\|EXCHANGING RESIN(2,1)\|EXPERIMENTAL WORK(2,1)\|EXTANT FARM EQUIPMENT(2,1)\|FILTRATE ANALYSIS(2,1)\|FULL SUMMATION(2,1)\|GRIND CELL(2,1)\|HEAVY PHOSPHATE(2,1)\|ICP ANALYSIS(2,1)\|IMMOBILIZATION(2,1)\|INDIGO CARBON(2,1)\|LABORATORY SETTING(2,1)\|MARINE SETTING(2,1)\|MINERAL DELIVERY(2,1)\|MINERAL DISSOLUTION RATE(2,1)\|NATURAL ABUNDANCE CALCULATION(2,1)\|NATURAL SOILS(2,1)\|NEGATIVE EMISSION(2,1)\|PHOSPHATE ZINC PRECIPITATE(2,1)\|PLANT DEMAND(2,1)\|PROJECT EVALUATION CRITERIA(2,1)\|RELEVANT ION(2,1)\|ROCK ELEMENTAL ANALYSIS(2,1)\|ROCK MATERIAL ACCELERATED WEATHERING(2,1)\|SAMPLING DENSITY(2,1)\|SHARP THRESHOLD(2,1)\|SOIL ELEMENTAL ANALYSIS(2,1)\|SUBSURFACE SOIL PORE WATER(2,1)\|TECHNOLOGICAL SOLUTION(2,1)\|WET GRAM(2,1)\|ABILITY THRESHOLD(1,1)\|ACCEPTANCE(1,1)\|ACCOUNTING(1,1)\|ACID TREATED ARTHROBACTER(1,1)\|ACIDIC SOIL SOLUTION(1,1)\|ADDITIONALITY(1,1)\|ADMIXTURE(1,1)\|AERATION(1,1)\|AGLIME MESH SIZE OBSERVATION(1,1)\|AGRICULTURE(1,1)\|ALGAL BLOOM(1,1)\|ANALYTICAL SOLUTION(1,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(1,1)\|ARACTUAI(1,1)\|ATTRACTION(1,1)\|AUTOCLAVE(1,1)\|BACTERIA(1,1)\|BIOADSORBED METAL ACTIVE RELEASE(1,1)\|BIOFUEL(1,1)\|CA BEARING SILICATE(1,1)\|CA CONTENT(1,1)\|CALIBRATION STANDARD(1,1)\|CAPTURING CARBON(1,1)\|CATION EXCHANGE COLUMN(1,1)\|CHARGE BALANCE(1,1)\|CHELATOR(1,1)\|CHITOSAN(1,1)\|CLASSIFICATION(1,1)\|CLAWBACK(1,1)\|CLIMEWORK(1,1)\|CO2 MOLECULAR MASS(1,1)\|\|(CA3207124)\|MINERAL AMENDMENT(100,28)\|ENHANCED ROCK(100,8)\|ENHANCED ROCK WEATHERING(100,2)\|SILICATE MINERAL AGGLOMERATION(51,2)\|COMMINUTED SILICATE MINERAL(44,3)\|INTERESTED PARTY(34,1)\|IMMOBILE TRACE ELEMENT(33,33)\|FUNDAMENTAL ISSUE(28,1)\|MINERAL TRANSFORMATION(24,2)\|ETHYLENE DIAMINE TETRAACETIC ACID(22,1)\|SAMPLING COLUMN(21,1)\|CARBON MEASUREMENT OBJECTIVE(20,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(18,1)\|LANDOWNER(18,1)\|SOIL SAMPLE(17,10)\|SLOW RELEASE ACIDIFIER(17,3)\|DIVALENT CATION MEASUREMENT(17,2)\|VERIFICATION(14,18)\|VANADIUM(14,2)\|BERYLLIUM(13,3)\|COMMERCIAL ENTERPRISE(13,1)\|DYSPROSIUM(12,10)\|GADOLINIUM(12,8)\|PRASEODYMIUM(12,7)\|GERMANIUM(12,3)\|RUBIDIUM(12,3)\|ZIRCONIUM(12,3)\|NEODYMIUM(11,12)\|EUROPIUM(11,11)\|LANTHANUM(11,10)\|SAMARIUM(11,9)\|SCANDIUM(11,9)\|YTTERBIUM(11,9)\|HOLMIUM(11,7)\|LUTETIUM(11,7)\|THULIUM(11,7)\|BINDER(11,3)\|GALLIUM(11,3)\|HAFNIUM(11,3)\|NIOBIUM(11,3)\|TANTALUM(11,3)\|GIBBSITE(11,2)\|RARE METAL(10,6)\|CESIUM(10,3)\|CHROMIUM(10,3)\|MINERAL AMENDMENT ADDITION(10,1)\|CERIUM(9,10)\|YTTRIUM(9,9)\|BRUKER PROPRIETARY GEO CALIBRATION(9,1)\|REMOVING CARBON(8,13)\|TRANSITION METAL(8,7)\|DRAWDOWN CALCULATION(8,4)\|VROCK MONTE CARLO SIMULATION(8,1)\|AVERAGE PARTICLE SIZE(7,4)\|ERW(7,4)\|BLAST FURNACE SLAG(7,2)\|CASO(7,2)\|RIGOROUS QUANTIFICATION(7,2)\|BIOLOGICAL DERIVED COMPONENT(7,1)\|DIVERSE DECARBONIZATION STRATEGY(7,1)\|PELLETIZED MINERAL AMENDMENT(7,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(7,1)\|RARE EARTH ELEMENT(6,20)\|PPB DETECTION(6,4)\|GYPSUM(6,3)\|MINERAL SOIL AMENDMENT(6,3)\|AIRTIGHT CONTAINMENT(6,2)\|NONLIMITING CANDIDATE(6,2)\|PHOSPHATE FERTILIZER(6,2)\|SI PERCENT MINERALOGICAL FRACTION(6,2)\|ALKALIZER KINETICS(6,1)\|DELIVER PROSPECTIVE REWARD(6,1)\|MINERAL ADDITIVE PROVEN IDENTITY(6,1)\|NEGATIVELY CHARGED BICARBONATE HCO(6,1)\|SOIL ORGANIC CARBON(6,1)\|STERILIZED SOIL BEAKER(6,1)\|TAXONOMY DISTINGUISHE(6,1)\|UNINHABITABLE WATERWAY(6,1)\|WET BIOMASS WET ALIQUOT(6,1)\|CARBON FLUX(5,3)\|INSTRUMENTAL ERROR(5,3)\|APPLIED DIVALENT CATION(5,2)\|COMPUTING VROCK(5,2)\|DISSOLUTION KINETICS(5,2)\|PULVERIZED SILICATE(5,2)\|ROCK PARTICLE(5,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(5,1)\|ALKALINITY EXPORT(5,1)\|BIODEGRADABLE TRANSPORTER(5,1)\|CO2 REAGENT AVAILABILITY(5,1)\|CUMULATIVE CATION FLUX MEASURE(5,1)\|HENRY LAW COEFFICIENT(5,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(5,1)\|INSTRUMENTAL UNCERTAINTY(5,1)\|MICRONUTRIENT INCORPORATION(5,1)\|MYCORRHIZAL INOCULUM(5,1)\|PELLET AGGLOMERATION(5,1)\|PORTABLE XRF INSTRUMENT(5,1)\|RESPIRATORY HEALTH IMPACT(5,1)\|NACL SOLUTION(4,4)\|PROMETHIUM(4,4)\|PULVERIZATION(4,4)\|TRIPLICATE(4,4)\|CENTRIFUGE CELL(4,3)\|CHARGE IMBALANCE(4,2)\|GROWING PLANT(4,2)\|INORGANIC ADDITIVE(4,2)\|MG PPM DETECTION(4,2)\|NEUTRAL GROUND(4,2)\|VROCK DOT PRODUCT(4,2)\|AEROSOL SIZED PARTICLE(4,1)\|AGGREGATED PELLET(4,1)\|AGGREGATING GROUND MINERAL(4,1)\|AGLIME SUBSTITUTE(4,1)\|AGRICULTURAL SOILS(4,1)\|AGRONOMIC PERFORMANCE EXPECTATION(4,1)\|ANALYTICAL LABORATORY(4,1)\|ANCIENT ROCK FORMATION(4,1)\|ANION CONSERVATION(4,1)\|BIOFILM MEDIATING(4,1)\|CATEGORY REGULATION(4,1)\|CATION CONSERVATION(4,1)\|CLAUSE XII(4,1)\|CO2 UPTAKE(4,1)\|DDIC DTA ESTIMATE(4,1)\|DIFFERENCE VROCK VECTOR(4,1)\|DISSOLVE ALGINATE(4,1)\|DISSOLVED ALGINATE POWDER(4,1)\|DOWNSTREAM ECOSYSTEM(4,1)\|DOWNSTREAM WATERWAY(4,1)\|DTA DH INVERSE(4,1)\|DUST PREVALENCE(4,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(4,1)\|FORSTERITE MOLE(4,1)\|FORSTERITE TENDENCY(4,1)\|FUNGAL ADJUVANT(4,1)\|GROUND MINERAL AGGREGATION(4,1)\|INFERRED ION FLUX(4,1)\|INTENSE SCRUTINY(4,1)\|KEY INSIGHT(4,1)\|MARKETING COLLATERAL(4,1)\|MICROBIAL CATION EXCHANGER(4,1)\|MINERAL ADJUVANT(4,1)\|NONPROFIT ORGANIZATION(4,1)\|NUTRIENT AVAILABILITY(4,1)\|OCEAN ACIDIFICATION(4,1)\|PELLET DISSOLUTION(4,1)\|PHOSPHATE ZINC PRECIPITATE(4,1)\|PHOSPHORUS ECOSYSTEM LOSS(4,1)\|PREAPPLICATION SOIL(4,1)\|PROGRESS FRACTIONATION(4,1)\|PROTONATED MICROBE(4,1)\|PULVERIZED LIMESTONE(4,1)\|PULVERIZED MG2SIO(4,1)\|QUASI GOVERNMENTAL REGULATOR(4,1)\|RENOWNED CHEMIST(4,1)\|RESERVOIR GEOLOGY(4,1)\|REWET BIOMASS(4,1)\|RIGOROUS COMPLIANCE(4,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(4,1)\|SOIL CULTIVATED ZONE(4,1)\|SOIL GEOCHEMISTRY(4,1)\|SOIL HYDROLOGY(4,1)\|SOIL STERILIZATION(4,1)\|SPECIALIZED TOOL(4,1)\|STEAM STERILIZATION(4,1)\|STYRENE DIVINYLBENZENE(4,1)\|TECHNO ECONOMIC MODELING(4,1)\|ULTIMATE PRICE(4,1)\|UREY REACTION BASIC PREMISE(4,1)\|VERIFICATION VERSION(4,1)\|VERIFIED ENHANCED ROCK(4,1)\|VOLUNTARY MARKET(4,1)\|X RAY FLUORESCENCE SPECTROSCOPY(4,1)\|CARBON DIOXIDE REMOVAL(3,10)\|AQUEOUS CO2(3,2)\|AVOIDED EMISSION(3,2)\|CARBONATE SPECIES(3,2)\|DISSOLVED CARBONATE(3,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(3,2)\|MARKET ABILITY(3,2)\|SECURE VESSEL(3,2)\|SOIL ENVIRONMENT(3,2)\|ABUNDANT CO2(3,1)\|ACCELERATE TIMING(3,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(3,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(3,1)\|AQUEOUS BICARBONATE MEASUREMENT(3,1)\|AQUEOUS COMPLEXATION(3,1)\|ASBESTOS EXPOSURE(3,1)\|ASSEMBLING MP(3,1)\|ATTENDANT DEMAND(3,1)\|AUXILIARY GEOCHEMICAL DATA(3,1)\|BICARBONATE MOLE(3,1)\|BROAD FRAMEWORK(3,1)\|CARBON EXCHANGE TRANSACTION(3,1)\|CARBON VERIFICATION BENEFIT(3,1)\|COARSE PARTICLE(3,1)\|COLLECT CELL PELLET(3,1)\|CONTINENTAL COLLISION RELEASE(3,1)\|CROP HEALTH(3,1)\|DISSOLUTION ENHANCING(3,1)\|DIVALENT MG(3,1)\|EQUILIBRIUM EQUATION(3,1)\|FERTILIZATION FREQUENCY(3,1)\|FRAUDULENT SAMPLE(3,1)\|GROUND NATURAL ENVIRONMENT(3,1)\|H2CO SUM(3,1)\|INCREASE ECOSYSTEM COBENEFIT(3,1)\|LB BROTH(3,1)\|MINERAL TRANSFORMATION EXTENT(3,1)\|MINUS PROTON DONOR(3,1)\|PHOSPHATE LEACHING(3,1)\|PHOSPHATE MOBILITY(3,1)\|PRECISE ANSWER(3,1)\|PREEQUILIBRATED TUBE(3,1)\|REACTION THERMODYNAMICS(3,1)\|SECURITIZED CARBON REMOVAL(3,1)\|SILICATE MINERAL SHELL(3,1)\|SILICATE ROLE(3,1)\|UNSEALING SAMPLE(3,1)\|VERIFIABLE CARBON REMOVAL(3,1)\|XRF ANALYSIS(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|VSOIT(2,3)\|BAG(2,2)\|CO2 REMOVAL(2,2)\|FARMER(2,2)\|PELLETIZING(2,2)\|PRODUCT FORMULATION(2,2)\|STAKEHOLDER(2,2)\|TOTAL FORMULATION(2,2)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC ENVIRONMENT(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL PERFORMANCE(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(2,1)\|CARBON MARKET MATURATION(2,1)\|CARBON REMOVAL VERIFICATION(2,1)\|CARBON TRANSACTION(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|COMPUTING INDEX(2,1)\|CORTEVA CARBON(2,1)\|DRIED PELLET(2,1)\|EMPLACEMENT LOCATION(2,1)\|ENTIRE US ECONOMY(2,1)\|EXCHANGE COEFFICIENT(2,1)\|EXCHANGING RESIN(2,1)\|EXPERIMENTAL WORK(2,1)\|EXTANT FARM EQUIPMENT(2,1)\|FILTRATE ANALYSIS(2,1)\|FULL SUMMATION(2,1)\|GRIND CELL(2,1)\|HEAVY PHOSPHATE(2,1)\|ICP ANALYSIS(2,1)\|IMMOBILIZATION(2,1)\|INDIGO CARBON(2,1)\|LABORATORY SETTING(2,1)\|MARINE SETTING(2,1)\|MINERAL DELIVERY(2,1)\|MINERAL DISSOLUTION RATE(2,1)\|MINERAL POTENTIAL(2,1)\|NATURAL ABUNDANCE CALCULATION(2,1)\|NATURAL SOILS(2,1)\|NEGATIVE EMISSION(2,1)\|PLANT DEMAND(2,1)\|PROJECT EVALUATION CRITERIA(2,1)\|RELEVANT ION(2,1)\|ROCK ELEMENTAL ANALYSIS(2,1)\|ROCK MATERIAL ACCELERATED WEATHERING(2,1)\|SAMPLING DENSITY(2,1)\|SHARP THRESHOLD(2,1)\|SOIL ELEMENTAL ANALYSIS(2,1)\|SUBSURFACE SOIL PORE WATER(2,1)\|TECHNOLOGICAL SOLUTION(2,1)\|WET GRAM(2,1)\|	(EP4256520)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising:\| measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and\| subsequently measuring the immobile trace elements in a soil sample after application of the mineral amendment to verify application of the mineral amendment,\| characterized in that the method comprises the steps of:\| determining the amount of the mineral amendment added to the soil sample,\| determining the amount of measured divalent cations in the soil sample,\| determining the fractional carbon dioxide removal by comparing the applied divalent cations to the measured divalent cations in the soil sample.\|2. The method of claim 1, wherein the immobile trace elements and magnesium are measured using inductively coupled plasma spectroscopy or x-ray fluorescence spectroscopy.\|3. The method of claim 1, further comprising the step of measuring the immobile trace elements in the soil sample prior to addition of the mineral amendment.\|4. The method of claim 1, further comprising the step of enriching the abundance of the immobile trace elements in the mineral amendment.\|5. The method of claim 1, wherein: the rare earth elements comprise scandium (Sc), yttrium (Y), lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm), europium (Eu), gadolinium (Gd), terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), and lutetium (Lu); the rare metals comprise beryllium (Be), cesium (Cs), gallium (Ga), germanium (Ge), hafnium (Hf), niobium (Nb), rubidium (Rb), tantalum (Ta), titanium (Ti), vanadium (V), and zirconium (Zr); and the transition metals comprise nickel (Ni), chromium (Cr), and zinc (Zn).\|6. The method of claim 1 wherein three immobile trace elements are measured.\|7. The method of claim 6, wherein the three immobile trace elements are selected from the list comprising: (Y', 'La', 'Ce'), (Y', 'La', 'Pr'), (Y', 'La', Nd'), (Y', 'La', 'Sm'), (Y', 'La', 'Eh'), (Y', 'La', 'Gd'), (Y', 'La', 'Tb'), (Y', 'La', 'Dy'), (Y', 'La', 'Ho'), (Y', 'La', 'Er'), (Y', 'La', 'Tm'), ('Y', 'La', 'Yb'), ('Y', 'La', 'Lu'), (Y', 'Ce', 'Pr'), (Y', 'Ce', 'Nd'), (Y', 'Ce', 'Sm'), ('Y', 'Ce', 'Eh'), (Y', 'Ce', 'Gd'), (Y', 'Ce', 'Tb'), (Y', 'Ce', 'Dy'), (Y', 'Ce', 'Ho'), (Y', 'Ce', 'Er'), (Y', 'Ce', 'Tm'), (Y', 'Ce', 'Yb'), (Y', 'Ce', 'Eh'), ('Y', 'Pr', 'Nd'), (Y', 'Pr', 'Sm'), (Y', 'Pr', 'Eu'), (Y', 'Pr', 'Gd'), (Y', 'Pr', 'Tb'), (Y', 'Pr', 'Dy'), (Y', 'Pr', 'Ho'), ('Y', 'Pr', 'Er'), ('Y', 'Pr', 'Tm'), ('Y', 'Pr', Yb'), ('Y', 'Pr', 'Eh'), (Y', Nd', 'Sm'), (Y', d', 'Eh'), (Y', Nd', 'Gd'), (Y', Nd', 'Tb'), (Y', Nd', Dy'), (Y', Nd', 'Ho'), (Y', Nd', 'Er'), (Y', Nd', 'Tm'), (Y', Nd', Yb'), (Y', Nd', 'Lu'), (Y', 'Sm', 'Eu'), (Y', 'Sm', 'Gd'), (Y', 'Sm', 'Tb'), (Y', 'Sm', 'Dy'), (Y', 'Sm', 'Ho'), ('Y', 'Sm', 'Er'), (Y', 'Sm', 'Tm'), (Y', 'Sm', Yb'), (Y, 'Sm', 'Lu'), (Y', 'Eu', 'Gd'), ('Y', 'Eu', 'Tb'), (Y', 'Eu', 'Dy'), (Y, 'Eu', 'Ho'), (Y', 'Eu', 'Er'), ('Y', 'Eu', 'Tm'), (Y', 'Eu', Yb'), ('Y', 'Eu', 'Lu'), (Y', 'Gd', 'Tb'), ('Y', Gd', 'Dy'), (Y', Gd', 'Ho'), (Y', 'Gd', 'Er'), (Y', 'Gd', 'Tm'), (Y, 'Gd', Yb'), (Y, 'Gd', 'Lu'), (Y', 'Tb', 'Dy'), (Y', 'Tb', 'Ho'), (Y', 'Tb', 'Er'), (Y', 'Tb', 'Tm'), (Y, 'Tb', Yb'), (Y', 'Tb', 'Lu'), (Y', 'Dy', 'Ho'), (Y', 'Dy', 'Er'), (Y, 'Dy', 'Tm'), (Y, 'Dy', Yb'), ('Y', Dy', 'Lu'), ('Y', 'Ho', 'Er'), (Y', 'Ho', 'Tm'), (Y', 'Ho', Yb'), (Y', 'Ho', 'Lu'), ('Y', 'Er', 'Tm'), (Y', 'Er', Yb'), (Y', 'Er', 'Lu'), (Y', 'Tm', Yb'), ('Y', 'Tm', 'Lu'), (Y', Yb', 'Lu'), ('La', 'Ce', 'Pr'), ('La', 'Ce', Nd'), ('La', 'Ce', 'Sm'), ('La', 'Ce', 'Eu'), ('La', 'Ce', 'Gd'), ('La', 'Ce', 'Tb'), ('La', 'Ce', Dy'), ('La', 'Ce', 'Ho'), ('La', 'Ce', 'Er'), ('La', 'Ce', 'Tm'), ('La', 'Ce', Yb'), ('La', 'Ce', 'Lu'), ('La', 'Pr', Nd'), ('La', 'Pr', 'Sm'), ('La', 'Pr', 'Eu'), ('La', 'Pr', Gd'), ('La', 'Pr', 'Tb'), ('La', 'Pr', 'Dy'), ('La', 'Pr', 'Ho'), ('La', 'Pr', 'Er'), ('La', 'Pr', 'Tm'), ('La', 'Pr', Yb'), ('La', 'Pr', 'Lu'), ('La', Nd', 'Sm'), ('La', Nd', 'Eu'), ('La', Nd', 'Gd'), ('La', Nd', 'Tb'), ('La', Nd', 'Dy'), ('La', Nd', 'Ho'), ('La', Nd', 'Er'), ('La', Nd', 'Tm'), ('La', Nd', Yb'), ('La', Nd', 'Lu'), ('La', 'Sm', 'Eu'), ('La', 'Sm', 'Gd'), ('La', 'Sm', 'Tb'), ('La', 'Sm', 'Dy'), ('La', 'Sm', 'Ho'), ('La', 'Sm', 'Er'), ('La', 'Sm', 'Tm'), ('La', 'Sm', Yb'), ('La', 'Sm', 'Lu'), ('La', 'Eu', Gd'), ('La', 'Eu', 'Tb'), ('La', 'Eu', Dy'), ('La', 'Eu', 'Ho'), ('La', 'Eu', 'Er'), ('La', 'Eu', 'Tm'), ('La', 'Eu', Yb'), ('La', 'Eu', 'Lu'), ('La', 'Gd', 'Tb'), ('La', 'Gd', 'Dy'), ('La', 'Gd', 'Ho'), ('La', 'Gd', 'Er'), ('La', 'Gd', 'Tm'), ('La', Gd', Yb'), ('La', Gd', 'Lu'), ('La', 'Tb', 'Dy'), ('La', 'Tb', 'Ho'), ('La', 'Tb', 'Er'), ('La', 'Tb', 'Tm'), ('La', 'Tb', Yb'), ('La', 'Tb', 'Lu'), ('La', 'Dy', 'Ho'), ('La', 'Dy', 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'Lu'), ('Ce', 'Gd', 'Tb'), ('Ce', 'Gd', 'Dy'), ('Ce', Gd', 'Ho'), ('Ce', 'Gd', 'Er'), ('Ce', 'Gd', 'Tm'), ('Ce', 'Gd', Yb'), ('Ce', 'Gd', 'Lu'), ('Ce', 'Tb', 'Dy'), ('Ce', 'Tb', 'Ho'), ('Ce', 'Tb', 'Er'), ('Ce', 'Tb', 'Tm'), ('Ce', 'Tb', Yb'), ('Ce', 'Tb', 'Lu'), ('Ce', 'Dy', 'Ho'), ('Ce', Dy', 'Er'), ('Ce', 'Dy', 'Tm'), ('Ce', 'Dy', Yb'), ('Ce', 'Dy', 'Lu'), ('Ce', 'Ho', 'Er'), ('Ce', 'Ho', 'Tm'), ('Ce', 'Ho', Yb'), ('Ce', 'Ho', 'Lu'), ('Ce', 'Er', 'Tm'), ('Ce', 'Er', Yb'), ('Ce', 'Er', 'Lu'), ('Ce', 'Tm', Yb'), ('Ce', 'Tm', 'Lu'), ('Ce', Yb', 'Lu'), ('Pr', 'Nd', 'Sm'), ('Pr', 'Nd', 'Eu'), ('Pr', 'Nd', Gd'), ('Pr', 'Nd', 'Tb'), ('Pr', 'Nd', Dy'), ('Pr', 'Nd', 'Ho'), ('Pr', Yd', 'Er'), ('Pr', Yd', 'Tm'), ('Pr', Yd', Yb'), ('Pr', Yd', 'Lu'), ('Pr', 'Sm', 'Eu'), ('Pr', 'Sm', 'Gd'), ('Pr', 'Sm', 'Tb'), ('Pr', 'Sm', Dy'), ('Pr', 'Sm', 'Ho'), ('Pr', 'Sm', 'Er'), ('Pr', 'Sm', 'Tm'), ('Pr', 'Sm', Yb'), ('Pr', 'Sm', 'Lu'), ('Pr', 'Eu', Gd'), ('Pr', 'Eu', 'Tb'), ('Pr', 'Eu', 'Dy'), ('Pr', 'Eu', 'Ho'), ('Pr', 'Eu', 'Er'), ('Pr', 'Eu', 'Tm'), ('Pr', 'Eu', Yb'), ('Pr', 'Eu', 'Lu'), ('Pr', Gd', 'Tb'), ('Pr', 'Gd', Dy'), ('Pr', 'Gd', 'Ho'), ('Pr', 'Gd', 'Er'), ('Pr', 'Gd', 'Tm'), ('Pr', 'Gd', Yb'), ('Pr', 'Gd', 'Lu'), ('Pr', 'Tb', 'Dy'), ('Pr', 'Tb', 'Ho'), ('Pr', 'Tb', 'Er'), ('Pr', 'Tb', 'Tm'), ('Pr', 'Tb', Yb'), ('Pr', 'Tb', 'Lu'), ('Pr', 'Dy', 'Ho'), ('Pr', 'Dy', 'Er'), ('Pr', Dy', 'Tm'), ('Pr', Dy', Yb'), ('Pr', 'Dy', 'Lu'), ('Pr', 'Ho', 'Er'), ('Pr', 'Ho', 'Tm'), ('Pr', 'Ho', Yb'), ('Pr', 'Ho', 'Lu'), ('Pr', 'Er', 'Tm'), ('Pr', 'Er', Yb'), ('Pr', 'Er', 'Lu'), ('Pr', 'Tm', Yb'), ('Pr', 'Tm', 'Lu'), ('Pr', Yb', 'Lu'), (Yd', 'Sm', 'Eu'), (Yd', 'Sm', 'Gd'), (Yd', 'Sm', 'Tb'), (Yd', 'Sm', 'Dy'), (Yd', 'Sm', 'Ho'), (Yd', 'Sm', 'Er'), (Yd', 'Sm', 'Tm'), (Yd', 'Sm', Yb'), (Yd', 'Sm', 'Lu'), (Yd', 'Eu', 'Gd'), (Yd', 'Eu', 'Tb'), (Yd', 'Eu', 'Dy'), (Yd', 'Eu', 'Ho'), (Yd', 'Eu', 'Er'), (Yd', 'Eu', 'Tm'), (Yd', 'Eu', Yb'), (Yd', 'Eu', 'Lu'), (Yd', 'Gd', 'Tb'), (Yd', 'Gd', 'Dy'), (Yd', 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'Ho', 'Er'), ('Sm', 'Ho', 'Tm'), ('Sm', 'Ho', Yb'), ('Sm', 'Ho', 'Lu'), ('Sm', 'Er', 'Tm'), ('Sm', 'Er', Yb'), ('Sm', 'Er', 'Lu'), ('Sm', 'Tm', Yb'), ('Sm', 'Tm', 'Lu'), ('Sm', Yb', 'Lu'), ('Eu', 'Gd', 'Tb'), ('Eu', 'Gd', 'Dy'), ('Eu', 'Gd', 'Ho'), ('Eu', 'Gd', 'Er'), ('Eu', 'Gd', 'Tm'), ('Eu', 'Gd', Yb'), ('Eu', 'Gd', 'Lu'), ('Eu', 'Tb', 'Dy'), ('Eu', 'Tb', 'Ho'), ('Eu', 'Tb', 'Er'), ('Eu', 'Tb', 'Tm'), ('Eu', 'Tb', Yb'), ('Eu', 'Tb', 'Lu'), ('Eu', 'Dy', 'Ho'), ('Eu', 'Dy', 'Er'), ('Eu', Dy', 'Tm'), ('Eu', Dy', Yb'), ('Eu', Dy', 'Lu'), ('Eu', 'Ho', 'Er'), ('Eu', 'Ho', 'Tm'), ('Eu', 'Ho', Yb'), ('Eu', 'Ho', 'Lu'), ('Eu', 'Er', 'Tm'), ('Eu', 'Er', Yb'), ('Eu', 'Er', 'Lu'), ('Eu', 'Tm', Yb'), ('Eu', 'Tm', 'Lu'), ('Eu', Yb', 'Lu'), ('Gd', 'Tb', Dy'), ('Gd', 'Tb', 'Ho'), ('Gd', 'Tb', 'Er'), ('Gd', 'Tb', 'Tm'), ('Gd', 'Tb', Yb'), ('Gd', 'Tb', 'Lu'), ('Gd', Dy', 'Ho'), ('Gd', 'Dy', 'Er'), ('Gd', 'Dy', 'Tm'), ('Gd', Dy', Yb'), ('GcT, 'Dy', 'Lu'), ('Gd', 'Ho', 'Er'), ('Gd', 'Ho', Tm1), (Gd', 'Ho', 'Yb'), ('Gd', 'Ho', 'Lu'), (Gd', 'Er', Tm'), ('Gd', 'Er', Yb'), ('Gd', 'Er', 'Lu'), ('Gd', 'Tm', Yb'), ('Gd', 'Tm', 'Lu'), ('Gd', Yb', 'Lu'), ('Tb', 'Dy', 'Ho'), ('Tb', 'Dy', 'Er'), ('Tb', 'Dy', 'Tm'), ('Tb', Dy', Yb'), ('Tb', 'Dy', 'Lu'), ('Tb', 'Ho', 'Er'), ('Tb', 'Ho', 'Tm'), ('Tb', 'Ho', Yb'), ('Tb', 'Ho', 'Lu'), ('Tb', 'Er', 'Tm'), ('Tb', 'Er', Yb'), ('Tb', 'Er', 'Lu'), ('Tb', 'Tm', Yb'), ('Tb', 'Tm', 'Lu'), ('Tb', Yb', 'Lu'), ('Dy', 'Ho', 'Er'), ('Dy', 'Ho', 'Tm'), ('Dy', 'Ho', Yb'), ('Dy', 'Ho', 'Lu'), ('Dy', 'Er', 'Tm'), ('Dy', 'Er', Yb'), ('Dy', 'Er', 'Lu'), ('Dy', 'Tm', Yb'), ('Dy', 'Tm', 'Lu'), ('Dy', Yb', 'Lu'), (Ho', 'Er', 'Tm'), (Ho', 'Er', Yb'), (Ho', 'Er', 'Lu'), (Ho', 'Tm', Yb'), (Ho', 'Tm', 'Lu'), (Ho', Yb', 'Lu'), ('Er', 'Tm', Yb'), ('Er', 'Tm', 'Lu'), ('Er', Yb', 'Lu'), and ('Tm', Yb', 'Lu').\|8. The method of claim 1, wherein the step of measuring the immobile trace elements in a soil sample after application of the mineral amendment further comprises lysing the soil sample and application of ethylenediaminetetraacetic acid.	(EP4256520)\|Cross Reference to Related Applications\|[0001] The present applications claims the priority benefit of U.S. Provisional Patent App. Serial No. 63/322,672, filed March 23, 2022; U.S. Provisional Patent App. Serial No. 63/289,395, filed December 14, 2021; and U.S. Provisional Patent App. Serial No. 63/213,398, filed, June 22, 2021.\|Background\|[0002] The last several years have witnessed a maturation of carbon markets from lightly scrutinized voluntary markets largely serving to provide positive marketing collateral to familiar consumer brands to rigorous compliance markets with proof-of-performance requirements often involving government and quasi-governmental regulators. There have also been a number of comprehensive proposals for decarbonization of the entire US economy, combining energy production, transportation, cement production, and agriculture. These proposals have included carbon dioxide removal (CDR) techniques as an essential component of the decarbonization plan, with a supportive ecosystem of science, policy, and project evaluation criteria. Within the diverse scope of decarbonization efforts, including renewable energy, biofuel, nature-based solutions, and more technical CDR techniques like direct air capture (DAC), The Oxford Principles have developed a taxonomy for categorizing diverse decarbonization strategies. This taxonomy distinguishes between avoided emissions (for instance, conversion of fossil fuel power to renewable power) and negative emissions (for instance direct air capture); distinguishes between avoided emissions that require storage (for instance carbon capture from a point source and sequestration into the ground) and those that do not require storage (the conversion to renewable energy); and the duration of the storage if so required (for instance, short lived forest carbon sequestration from delayed harvests versus storage of captured carbon in geological formations).\|[0003] A number of for-profit and non-profit organizations have emerged that employ the Oxford Principles to evaluate proposals, particularly around the rigorous quantification across categories (Table 1). This, in essence, is the scorecard that projects will have to compete on to find acceptance in the industry. All other things equal, cost ends up being the primary driver, but quality is also a key consideration. Thus, historically buyers have been drawn to nature-based solutions that cost between $5-20/tCO2 e (e.g., Corteva Carbon, Indigo Carbon), versus direct air capture projects that cost >$500/tCO2 e (e.g., ClimeWorks). However, there are challenges to these nature-based solutions: recently these nature-based solutions have been subject to intense scrutiny for "gaming" the rules or otherwise failing to deliver prospective rewards. Among the technological solutions, there are a different set of challenges: rigor has been strong, but the reduction in price proportional to increase in deployment has been slow, and the ultimate price of DAC is not expected to drop below $150/tCO2e (Keith et al 2018, https://doi.org/10.1016/j.joule.2018.05.006). In light of these challenges, we have developed a technology around "enhanced rock weathering" (ERW), in which silicate minerals are weathered in acidic soil solution, thus driving the uptake of additional CO2 into dissolved inorganic carbon (DIC) in the soil solution. Our experimental work, life cycle analysis, and techno-economic modeling have indicated that ERW provides the permanence, additionality, and rigorous quantification of a DAC project, the large volume of a carbon capture and storage (CCS) project, and the unit economics of a nature based solution, thus creating a new tool to meet net-zero goals.\|Details of Enhanced Rock Weathering\|[0004] In "enhanced rock weathering" (ERW), silicate minerals are weathered by CO2 from the ambient air which has been dissolved into water, reacting to produce dissolved inorganic carbon that is ultimately stored in the ocean as depicted in FIGS. 1 and 2.\|Background Geochemistry\|[0005] The role of silicate rock weathering in maintaining the CO2 balance of the atmosphere has been recognized for decades, first outlined by renowned chemist Harold Urey in the 1950s. The basic premise of the Urey reaction is that continental collisions release CO2 to the atmosphere from volcanoes, and bring Mg- and Ca-bearing silicate rocks to the surface. The rainwater (H2O) that falls upon these rocks is mildly acidic, as atmospheric CO2 has dissolved in it and formed carbonic acid (H2CO3). For forsterite, the weathering reaction takes place following the form:\| Mg2SiO4 + 4 H2O + 4 CO2 → 2 Mg2+ + 4 HCO3- + 4 H4SiO4\|[0006] In this reaction, one mole of forsterite consumes four moles of CO2, so two negatively charged bicarbonate HCO3- are created for every one divalent Mg2+ weathered. Given the molecular weight of forsterite (140 g/mol) and the molecular weight of CO2 (44 g/mol), weathering one metric ton of forsterite removes 1.25 metric tons of CO2 from the atmosphere. In general, such a formula can be used to define the "mineral potential" of a silicate based on its elemental composition: \| where V is the valence of the cation (2 for Mg and Ca) and MW is the molecular weight.\|[0007] The rate of weathering is determined by the surface area of the mineral, the acidity (pH) of the soil solution, the temperature of the solution, the availability of CO2 reagent in solution, and the rate of removal of the reaction products by water. One of the key insights into the potential of "enhanced" rock weathering is that the rate of reaction, and thus CO2 removal, can be greatly accelerated by increasing the surface area by pulverization into a fine powder (e.g., less than 100 um), incorporating into an acidic environment (e.g., pH less than 6) with abundant CO2 present, and with steady water flux to remove reaction products to maintain acidity. While this formula defines the potential amount of CO2 that may be removed by weathering, it does not speak to the rate; ancient rock formations testify that the rate of weathering can be extremely slow.\|[0008] The relationship between silicates (like Mg2SiO4) and dissolved carbonates (like HCO3-) is not necessarily intuitive, as the carbonate system of water involves a number of coupled reactions. Atmospheric CO2 dissolves into water according to an exchange coefficient:\| CO2(aq) = H2CO3 = KCO2 * pCO2\|[0009] Technically pCO2 is "fugacity" that represents its activity, but, as used herein, it is more or less equivalent to its partial pressure, and KCO2 is the Henry's law coefficient that determines the aqueous CO2 in equilibrium with the atmosphere. This aqueous CO2 in turn hydrates with H2O to become carbonic acid (H2CO3), which dissociates to become bicarbonate (HCO3-) and carbonate (CO32-):\| H2CO3 ↔ HCO3- + H+\| HCO3- ↔ CO32- + H+\|[0010] These equilibrium reactions are defined by K1 and K2, the first and second carbonate system dissociation constants. pK1 and pK2 are about 5.9 and about 9.4 at STP, so greater than 99% of the charge in the dissolved carbonates is HCO3-.\|[0011] The carbonates are the largest constituents of total alkalinity, which is defined as the charge imbalance between weak acids (proton acceptors) minus proton donors:\| TA = [HCO3-] + 2 · [CO32-] + [OH-] - [H+]\|[0012] There is an alternative definition of total alkalinity as the charge imbalance between conserved cations and conserved anions:\| TA = [Na+] + 2 [Mg2+] + 2 [Ca2+] + [K+] + ... - [Cl-] - 2 [SO42-] - [NO3-]\|[0013] These two expressions are always equal (i.e. the charges balance). This means that an added Mg or Ca into soil solution will increase in HCO3- to balance the charge. We describe an analytical solution to compute how much carbon is taken up per unit of additional Mg or Ca. If we first define DIC as the sum of H2CO3, HCO3-, and CO32-, and make use of the equilibrium equations above (defining H+ as "h" and H2CO3 as "s"): \|[0014] And formulate TA using the same convention: \|[0015] With these definitions in place, we can develop an estimate of dDIC/dTA. First, we compute the derivative dTA/dh: \|[0016] Next we compute the derivative dDIC/dh: \|[0017] Finally we multiply dDIC/dh by the inverse of dTA/dh to calculate dDIC/dTA: \|[0018] At the pH found in soils, each Mg or Ca is matched by two carbon atoms. In all circumstances, raising alkalinity results in increased pH. This is particularly important in marine settings, where ocean acidification from increased atmospheric CO2 can be ameliorated by this export of alkalinity from land.\|[0019] The potential for ERW as a commercial enterprise is limited by some fundamental issues:\| A. The total amounts of mineral transformation and carbon removal should be verifiable empirically. The verification methods described below may be low cost at scale, can be performed at arm's length by a 3rd party, and may have safeguards to eliminate fraud.\|[0020] Additionally, the commercial potential for ERW could be enhanced by a number of different features. Embodiments may include:\| B. Processes and modifications of the engineered mineral product that enhance the agronomic performance and ecosystem co-benefits of the engineered mineral.\| C. Processes and modifications of the engineered mineral product that control or enhance the mineral dissolution rate of the engineered mineral in soil environments and thus the rate of removal of CO2.\| C. Paulo et al, Applied Geochemistry, 2021, 219, 104955, discusses evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralisation.\| N. Moosdorf et al, Environ. Sci. Tech., 2014, 48, 4809 discusses carbon dioxide efficiency of terrestrial enhanced weathering and determination of effective carbon dioxide sequestration.\|Brief Description of the Drawings\|[0021] FIG. 1 is a drawing illustrating the enhanced rock weathering cycle.\| FIG. 2 is a graph depicting the effect of comminution on dissolution kinetics for a silicate.\| FIGS. 3A to 3D are graphs depicting the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um which closely approximates the alkalinity release dynamics for aglime.\| FIG. 4 is a drawing illustrating the general scheme for a verified enhanced rock weathering cycle.\|Detailed Description\|[0022] Summary: The following described methodologies can establish one version of a verification scheme that will demonstrate the transformation of the applied rock material and the subsequent carbon removal into secure geologic reservoirs as evidenced by observations collected from the soil. One set of methods (A) can measure the production of free ions from the applied material and the transport of those ions outside of a control volume as a direct measure of the amount of weathering and thus total carbon dioxide equivalent isolated from the atmosphere. Furthermore, as the elemental inputs into the soil induced by enhanced rock weathering can have significant effects on the soil geochemistry, methods in (B) describe systems and versions that can enhance the agronomic performance of the soil amendment and increase ecosystem co-benefits. Lastly, methods in (C) elaborate on versions that control and enhance the mineral dissolution rate, which increases the financial performance of enhanced rock weathering technology in the marketplace.\| A. Systems and methods for monitoring and verification:Described below are several example methodologies for quantifying the rate and extent of mineral transformation and carbon removal, which are referred to as "verification methodologies".1. Example Verification methodology 1:a. A cation exchange resin and/or an anion exchange resin are packaged into a physical embodiment (such as a 5 cm diameter tube, 5cm in length, placed 30 cm below the soil surface) that allows vertical transport of fluids but not horizontal transport.\| b. Commercial ion exchange resins are pre-equilibrated in such a way that their selectivity is high for the relevant ions, but their capacity is also sufficiently high such that saturation is minimized. This technology may allow for effective deployment for long periods of time, allowing passage of up to 4000 mm of moisture through the tube, without becoming saturated with respect to the ions of interest.\| c. The ions of interest are restricted to divalent cations (Mg2+, Ca2+), carbonate species (HCO3- and CO32-), and silicic acid (H4SiO4), important weathering products of preferred mineral soil amendments, such as ultramafic rocks, blast furnace slag, and other naturally occurring or industrial silicate minerals with high Mg and Ca content.\| d. Three pre-equilibrated tubes are emplaced fully under the soil below a control depth (e.g., 30 cm, a typical depth of cultivation). This may be done by removing the top 30 cm soil with a shovel or auger, then gently placing the tube in the created void space. Following a certain period of time post-surface application of mineral soil amendment (e.g., 9 to 12 months after application), the tubes are retrieved, and the ions captured within the resin exchanges are measured using standard methodologies, such as ICP-OES and ICP-MS based concentration measurements. Three tubes are used to determine standard deviation error in triplicate.\| e. By the principle of charge balance and known thermodynamic reactions taking place in the top 30 cm of soils, the amount of carbonate can be inferred purely from the measurement of cations, under certain assumptions and auxiliary geochemical data. By the addition of more specific anion exchange resins, such as styrenedivinylbenzene, these assumptions can be avoided to get a more precise answer. The increase in cation concentration in the subsurface soil pore water allows for the stoichiometric determination of carbon removal from the gas phase (ambient air).\| f. The total carbon dioxide removed during the deployment period may be estimated as equal to the molecular mass of CO2 (44 g/mol) multiplied by the sum of the number of moles of carbonate and two times the number of moles of bicarbonate, multiplied by the area on which mineral was applied to the field, divided by the cross-sectional area of the tube.\| g. Direct measurement of aqueous bicarbonate and carbonate species, which are the most readily available forms of carbon induced by a gas exchange of carbon dioxide with the soil pore water, may be conducted using the specified anion exchange resin above. The expression as described in clause (f) explains the calculation used to convert this direct measurement of carbon to an absolute value of carbon dioxide removed during a specified application period.\| h. Verification methodology 1 has the advantage that it can provide a direct measure of carbon flux and employs a measurement technique that is mature.\| i. However, potential disadvantages may include the need for manufacturing (and its attendant demand for working capital); devices may occasionally be defective; emplacement of a device may alter the flow paths of water, which in turn alters the inferred ion fluxes; emplacement of a device may depend on the user; the knowledge of the location of emplacement may invite manipulation by a stakeholder involved in a carbon transaction; and others. 2. Example Verification methodology 2:a. The principle behind Verification methodology 2 is that minerals applied for purposes of enhanced rock weathering contain, in addition to the elements outlined above that participate in the weathering reaction (i.e., magnesium, calcium, iron, silicon, oxygen, hydrogen), additional elements in trace amounts. These additional trace elements (TEs) might include rare earth elements (REEs), rare metals (RM), other transition metals (TMs), or a combination thereof. Unlike the primary weathering products that are readily dissolved in solution and lost by leaching, some TEs are strongly bound to mineral and biological surfaces and do not readily leach from the soil control volume (e.g., the top 10 to 30 cm of soil), and are not removed by plants at the concentrations present in our applied rock. These strongly bound trace elements are referred to herein as immobile trace elements (ITEs). Thus, a measure of cumulative cation flux and carbon removal can be computed by comparing the ratio of the lost weathering products, such as magnesium, to ITEs, after accounting for background concentrations of ITEs in the initial soil.\| b. As used herein, rare earth elements include scandium (Sc), yttrium (Y), lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm), europium (Eu), gadolinium (Gd), terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), lutetium (Lu) or a combination thereof. As used herein, rare metals include beryllium (Be), cesium (Cs), gallium (Ga), germanium (Ge), hafnium (Hf), niobium (Nb), rubidium (Rb), tantalum (Ta), zirconium (Zr), or a combination thereof. As used herein, transition metals include nickel (Ni), chromium (Cr), and zinc (Zn) among others and may include a combination of transition metals.\| c. An approach based on ITEs depends on the degree of immobility of the element in soil environments, the time horizon after which the ITEs will be measured to estimate carbon removal, the abundance of ITEs in both the soil and the mineral added, and the analytical chemistry used to measure this abundance. An analytical technique that has low detectability thresholds for slightly mobile elements could be sufficient for relatively abundant (e.g., parts per thousand to parts per million) elements over short time horizons (e.g., weeks to months). On the other hand, a different analytical technique could be used over longer time horizons, which in turn could involve quantification of very immobile elements that are present in much lower abundance (e.g., parts per billion to parts per trillion). The approach may be chosen based at least in part on cost, which ITEs are actually conserved, over which time horizons, as well as the performance of the analytical performance used.\| d. The relative proportions of ITEs in a sample (rock or soil) constitute a type of unique fingerprint of the material. Because the cost of pure ITEs is large, and the analytical chemistry is not widely available, there is a significant barrier to engineering a fraudulent sample to reproduce the native ITE fingerprint of a mineral soil amendment. Thus, it would be challenging for a stakeholder in a carbon exchange transaction to generate a result that produces the anticipated result (a high or low amount of carbon removal) while also matching the ITE fingerprint generated by a bona fide sample. This is a contrast with measurement schemes for soil organic carbon, in which the landowner or other interested party has an information advantage in terms of where or when to sample, which could be used to achieve a particular carbon measurement objective (high or low).\| e. Verification Methodology 2 (VM2) has advantages over Verification Methodology 1 (VM1) in that it avoids the need for the use of a device, which avoids altering the soil hydrology or physical environment in a way that would impact the observed elemental analysis.\| f. VM2 may have an advantage over VM1 in not requiring tracking of a specific location for recovering the sampling column.\| g. VM2 does, however, include measurement techniques that are less widely available; requires specialized instruments and personnel; requires additional boundary conditions to compute carbon flux (e.g., pre-application soil and rock elemental analysis); and employs assumptions as to the relationship between cation flux and carbon flux.\| h. Like VM1, VM2 uses the total amount of mineral applied and the field area, which could be measured, for example, using a digital as-applied map commonly accompanying crops input machinery, or truck weights before and after mineral delivery. This will be referred to as the nominal application rate (ARnominal).\| i. There are four main calculations in VM2. To the extent any one of these factors is known unambiguously from other sources, each step in VM2 could be used in isolation from the others.i. Classify, using ITE fingerprinting, whether a soil has had a specific mineral applied, which may be asserted by an entity wishing to make a claim;\| ii. Calculate, using ITE fingerprinting, what the actual mineral application rate (ARactual) for a specific soil sample was, which will necessarily differ in a systematic or random way from the average rate for the entire field;\| iii. Calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the application rate in (ii) above;\| iv. Calculate, using the fraction computed in (iii) and the mineral potential (Equation 1) computed for the feedstock identified in (i) above, the amount of carbon dioxide removed. j. In one non-limiting embodiment, the verification methodology to classify whether the claimed mineral applied is the actual mineral applied is as follows:i. Collect a sample from mineral to be applied, place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Mineral Amendment.\| ii. Prior to mineral application, collect a 20 g sample from cultivated zone of soil (typically at around 30 cm, such as in a range of 0 cm to 30 cm), place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Soil A.\| iii. Subsequent to mineral application, collect a 20 g sample the same control zone as soil A, and store under similar conditions. Label as Soil B. Soil B could be sampled immediately after mineral application or at a later time (e.g., months to years afterwards).\| iv. Characterize the elemental composition of Mineral Amendment, Soil A, and Soil B. Example approaches to characterizing the elemental composition are described in (v) and (vi).\| v. One approach to measuring the elemental composition is as follows:1. In a laboratory setting, unseal the soil samples and place 10 grams of Soil A and Soil B in two separate beakers.\| 2. Dissolve the solids in strong acid. For example, add 21 mL of strong 1.0 M hydrochloric acid and 7 mL of strong 1.0 M nitric acid (total 28 mL acid) to each beaker of sterilized soil and stir rigorously until solids are dissolved.\| 3. Filter the sample-containing beakers first through a 1- to 5-micron water filter cartridge followed by an attached 10 to 20 cm column cation exchange resin at a sufficiently slow flow rate of, for example, 1 to 5 mL/min. This combination of a water filter with a cation exchange column has been engineered for optimal performance with soils under consideration. Specifically, the 5-micron water filter cartridge separates out any larger particles, allowing for the smaller particles to exchange its bound metals with the subsequent cation exchange resin.\| 4. Flush copious amounts (e.g., 100-200 mL) of 0.5 to 1.0 M chelator such as, for example, ethylenediaminetetraacetic acid (EDTA) at 1-5 mL/min through the used filters into their respective filtrates. This may collect any additional metals that were still adhered to the filters.\| 5. Send filtrate A (resultant sample from Soil A) and filtrate B (resultant sample from Soil B) to an analytical laboratory for analysis on an inductively coupled plasma mass spectrometer (ICP-MS). Measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3.\| 6. The ICP-MS may be set to detect magnesium concentrations and the following 17 elements on a high ppb or low ppm detection level: Yttrium, Scandium, Lanthanum, Cerium, Praseodymium, Neodymium, Promethium, Samarium, Europium, Gadolinium, Terbium, Dysprosium, Holmium, Erbium, Thulium, Ytterbium, Lutetium. Classify light rare earth elements (LREEs) as yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium. Classify heavy rare earth elements (HREEs) as europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium. Send an isolated rock material sample for ICP-MS analysis. Similar to the filtrate analyses, measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3. vi. Another approach to measuring the elemental composition is as follows:1. Calibrate a portable XRF instrument for particularly low detection limit of ITEs using a calibration standard (such as Bruker proprietary Geo calibration + custom ITE standards).\| 2. Use the portable XRF instrument to analyze the Rock Material and Soil A for ITEs (as identified in Verification methodology 2), reporting the instrumental error (2 standard deviations) as well.\| 3. Use the portable XRF instrument to analyze Soil B for ITEs, reporting the instrumental error (2 standard deviations) as well. vii. Once the above elemental composition has been determined, calculate the difference for every element between Mineral Amendment and Soil A, resulting in a vector of differences vrock. Likewise, compute the difference for every element between Soil B and Soil A, resulting in a vector of differences vsoil. To improve performance, each element may be divided by an individual factor, such as the detection threshold, or the instrumental uncertainty, or the elemental composition of a reference material. Another means to improve performance would be to sum a subset of the elements or several distinct subsets of elements before computing vrock and vsoil. Another means to improve performance would be to compute indices of these summed subsets of elements, for example the ratio of the light REEs to the heavy REEs, before computing vrock and vsoil.\| viii. Compute the dot product of vrock and vsoil. If the value of this dot product is close to 1 (e.g., within a threshold value), then the Soil B is positively classified as having the Mineral Amendment. If the value of the dot product is less than 1 minus a threshold value, then Soil B is negatively classified as not having the Mineral Amendment.\| ix. The threshold value may be determined using a variety of means, for example the half-angle between the dot product of vrock and vsoil and any other known vrock and vsoil; or using a Monte Carlo simulation of vrock and vsoil that accounts for known sources of uncertainty including instrumental error, variation in rock elemental analysis, or variation of soil elemental analysis. k. In one non-limiting embodiment, the verification methodology to calculate the actual mineral application rate (ARactual) for a specific soil sample is as follows:i. Characterize the elemental composition the elemental composition of Mineral Amendment, Soil A, and Soil B as above. Note that there could be different analytical chemistry employed if, for example, rapid and inexpensive XRF analysis was used for classification soon after application, and slower and more costly ICP analysis may be used to estimate application rates.\| ii. Compute the differences in elemental composition as above, potentially including similar performance enhancements such as normalizing by factors specific to each element, summing across subsets of elements, and computing indices such as the ratio of light REEs to heavy REEs. Such transformed and summed variables for a sample will be referred to generically as ΣITEsample.\| iii. The actual application rate of the sample can be calculated using the following expression: l. In one non-limiting embodiment, the verification methodology to calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the actual mineral application rate (ARactual) as follows:i. The amount of divalent cations applied (DCapplied) can be calculated by the proven identity of the mineral additive and the actual application rate: where divalent cations are generally restricted in this context to Mg and Ca, and Mgmineral and Camineral is the fractional composition of the mineral additive.\| ii. The amount of divalent cations remaining (DCremain) in the soil could be estimated using the same elemental analysis as previously (if, for example, ICP-MS was used), or determined from the same sample using a different analysis (if, for example XRF was used and Mg was not measured).\| iii. The fractional progress of carbon dioxide removal (CDR) can be estimated by the ratio of remaining divalent cations to applied divalent cations: m. In one non-limiting embodiment, the verification methodology to calculate the amount of carbon dioxide removed from the control volume is as follows:i. Assembling MP, fCDR , ARnominal and the land area applied, the total carbon dioxide removal is: n. While Verification Methodology 2 presented herein provides a broad framework for the detection and application of soil-bound ITEs to estimate long-term geologic carbon drawdown, the efficacy of the approach can also be improved through the focus on specific subsets of ITEs. Non-limiting embodiments of such improvements are listed below:i. The ITEs specified in equation 2, e.g., (ΣITEssoil B), may in fact be represented not by the full summation of 17 REEs but instead by the use of only LREEs or the use of only HREEs, as defined in clause xii. Such a calculation would mean the sum of only LREEs in the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium) or the sum of only HREEs in the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium).\| ii. Within the use of only LREEs for the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium), some LREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual LREEs are selected. For example, the subset may include three LREEs. The calculation (equation 2) is conducted for each of the 3 LREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 LREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [yttrium, scandium, lanthanum], [cerium, lanthanum, neodymium], [cerium, neodymium, samarium], [yttrium, cerium, neodymium], [scandium, neodymium, samarium].\| iii. Within the use of only HREEs for the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium), some HREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual HREEs are selected. For example, the subset may include three HREEs. The calculation (equation 2a) is conducted for each of the 3 HREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 HREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [europium, gadolinium, terbium], [europium, terbium, dysprosium], [dysprosium, erbium, ytterbium], [europium, erbium, ytterbium], [europium, dysprosium, erbium].\| iv. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual REEs are selected. For example, the subset may include three REEs Chart 1 represents a non-limiting list of REE triplicates that may enhance the efficacy of this C drawdown calculation.Chart 1. A non-limiting list of 455 REE triplicates that can be used to effectively triangulate a C drawdown estimation\|('Y', 'La', 'Ce'), ('Y', 'La', 'Pr'), ('Y', 'La', 'Nd'), ('Y', 'La', 'Sm'), ('Y', 'La', 'Eu'), ('Y', 'La', 'Gd'), ('Y', 'La', 'Tb'), ('Y', 'La', 'Dy'), ('Y', 'La', 'Ho'), ('Y', 'La', 'Er'), ('Y', 'La', 'Tm'), ('Y', 'La', 'Yb'), ('Y', 'La', 'Lu'), ('Y', 'Ce', 'Pr'), ('Y', 'Ce', 'Nd'), ('Y', 'Ce', 'Sm'), ('Y', 'Ce', 'Eu'), ('Y', 'Ce', 'Gd'), ('Y', 'Ce', 'Tb' ), ('Y', 'Ce', 'Dy'), ('Y', 'Ce', 'Ho'), ('Y', 'Ce', 'Er'), ('Y', 'Ce', 'Tm'), ('Y', 'Ce', 'Yb'), ('Y', 'Ce', 'Lu'), (' Y', 'Pr', 'Nd'), ('Y', 'Pr', 'Sm'), ('Y', 'Pr', 'Eu'), ('Y', 'Pr', 'Gd'), ('Y', 'Pr', 'Tb'), ('Y', 'Pr', 'Dy'), ('Y', 'Pr ', 'Ho'), ('Y', 'Pr', 'Er'), ('Y', 'Pr', 'Tm'), ('Y', 'Pr', 'Yb'), ('Y', 'Pr', 'Lu'), ('Y', 'Nd', 'Sm'), ('Y', 'Nd', 'E u'), ('Y', 'Nd', 'Gd'), ('Y', 'Nd', 'Tb'), ('Y', 'Nd', 'Dy'), ('Y', 'Nd', 'Ho'), ('Y', 'Nd', 'Er'), ('Y', 'Nd', 'Tm' ), ('Y', 'Nd', 'Yb'), ('Y', 'Nd', 'Lu'), ('Y', 'Sm', 'Eu'), ('Y', 'Sm', 'Gd'), ('Y', 'Sm', 'Tb'), ('Y', 'Sm', 'Dy'), ('Y', 'Sm', 'Ho'), ('Y', 'Sm', 'Er'), ('Y', 'Sm', 'Tm'), ('Y', 'Sm', 'Yb'), ('Y', 'Sm', 'Lu'), ('Y', 'Eu', 'Gd'), ('Y', 'Eu', 'Tb'), ('Y', 'Eu', 'Dy'), ('Y', 'Eu', 'Ho'), ('Y', 'Eu', 'Er'), ('Y', 'Eu', 'Tm'), ('Y', 'Eu', 'Yb'), ('Y ', 'Eu', 'Lu'), ('Y', 'Gd', 'Tb'), ('Y', 'Gd', 'Dy'), ('Y', 'Gd', 'Ho'), ('Y', 'Gd', 'Er'), ('Y', 'Gd', 'Tm'), ('Y', ' Gd', 'Yb'), ('Y', 'Gd', 'Lu'), ('Y', 'Tb', 'Dy'), ('Y', 'Tb', 'Ho'), ('Y', 'Tb', 'Er'), ('Y', 'Tb', 'Tm'), ('Y', 'Tb ', 'Yb'), ('Y', 'Tb', 'Lu'), ('Y', 'Dy', 'Ho'), ('Y', 'Dy', 'Er'), ('Y', 'Dy', 'Tm'), ('Y', 'Dy', 'Yb'), ('Y', 'Dy', 'Lu'), ('Y', 'Ho', 'Er'), ('Y', 'Ho', 'Tm'), ('Y', 'Ho', 'Yb'), ('Y', 'Ho', 'Lu'), ('Y', 'Er', 'Tm'), ('Y', 'Er', 'Y b'), ('Y', 'Er', 'Lu'), ('Y', 'Tm', 'Yb'), ('Y', 'Tm', 'Lu'), ('Y', 'Yb', 'Lu'), ('La', 'Ce', 'Pr'), ('La', 'Ce', 'Nd' ), ('La', 'Ce', 'Sm'), ('La', 'Ce', 'Eu'), ('La', 'Ce', 'Gd'), ('La', 'Ce', 'Tb'), ('La', 'Ce', 'Dy'), ('La', 'Ce', ' Ho'), ('La', 'Ce', 'Er'), ('La', 'Ce', 'Tm'), ('La', 'Ce', 'Yb'), ('La', 'Ce', 'Lu'), ('La', 'Pr', 'Nd'), ('La', 'Pr', 'Sm'), ('La', 'Pr', 'Eu'), ('La', 'Pr', 'Gd'), ('La', 'Pr', 'Tb'), ('La', 'Pr', 'Dy'), ('La', 'Pr', 'Ho'), ('La', 'Pr', ' Er'), ('La', 'Pr', 'Tm'), ('La', 'Pr', 'Yb'), ('La', 'Pr', 'Lu'), ('La', 'Nd', 'Sm'), ('La', 'Nd', 'Eu'), ('La', 'Nd', 'Gd'), ('La', 'Nd', 'Tb'), ('La', 'Nd', 'Dy'), ('La', 'Nd', 'Ho'), ('La', 'Nd', 'Er'), ('La', 'Nd', 'Tm'), ('La', ' Nd', 'Yb'), ('La', 'Nd', 'Lu'), ('La', 'Sm', 'Eu'), ('La', 'Sm', 'Gd'), ('La', 'Sm', 'Tb'), ('La', 'Sm', 'Dy'), (' La', 'Sm', 'Ho'), ('La', 'Sm', 'Er'), ('La', 'Sm', 'Tm'), ('La', 'Sm', 'Yb'), ('La', 'Sm', 'Lu'), ('La', 'Eu', 'G d'), ('La', 'Eu', 'Tb'), ('La', 'Eu', 'Dy'), ('La', 'Eu', 'Ho'), ('La', 'Eu', 'Er'), ('La', 'Eu', 'Tm'), ('La', 'Eu', ' Yb'), ('La', 'Eu', 'Lu'), ('La', 'Gd', 'Tb'), ('La', 'Gd', 'Dy'), ('La', 'Gd', 'Ho'), ('La', 'Gd', 'Er'), ('La', 'G d', 'Tm'), ('La', 'Gd', 'Yb'), ('La', 'Gd', 'Lu'), ('La', 'Tb', 'Dy'), ('La', 'Tb', 'Ho'), ('La', 'Tb', 'Er'), ('La', 'Tb', 'Tm'), ('La', 'Tb', 'Yb'), ('La', 'Tb', 'Lu'), ('La', 'Dy', 'Ho'), ('La', 'Dy', 'Er'), ('La', 'Dy', 'Tm'), ('L a', 'Dy', 'Yb'), ('La', 'Dy', 'Lu'), ('La', 'Ho', 'Er'), ('La', 'Ho', 'Tm'), ('La', 'Ho', 'Yb'), ('La', 'Ho', 'Lu'), ('La', 'Er', 'Tm'), ('La', 'Er', 'Yb'), ('La', 'Er', 'Lu'), ('La', 'Tm', 'Yb'), ('La', 'Tm', 'Lu'), ('La', 'Yb', 'Lu' ), ('Ce', 'Pr', 'Nd'), ('Ce', 'Pr', 'Sm'), ('Ce', 'Pr', 'Eu'), ('Ce', 'Pr', 'Gd'), ('Ce', 'Pr', 'Tb'), ('Ce', 'Pr', 'Dy' ), ('Ce', 'Pr', 'Ho'), ('Ce', 'Pr', 'Er'), ('Ce', 'Pr', 'Tm'), ('Ce', 'Pr', 'Yb'), ('Ce', 'Pr', 'Lu'), ('Ce', 'Nd', 'Sm '), ('Ce', 'Nd', 'Eu'), ('Ce', 'Nd', 'Gd'), ('Ce', 'Nd', 'Tb'), ('Ce', 'Nd', 'Dy'), ('Ce', 'Nd', 'Ho'), ('Ce', 'Nd', 'Er'), ('Ce', 'Nd', 'Tm'), ('Ce', 'Nd', 'Yb'), ('Ce', 'Nd', 'Lu'), ('Ce', 'Sm', 'Eu'), ('Ce', 'Sm', 'Gd'), ('Ce', ' Sm', 'Tb'), ('Ce', 'Sm', 'Dy'), ('Ce', 'Sm', 'Ho'), ('Ce', 'Sm', 'Er'), ('Ce', 'Sm', 'Tm'), ('Ce', 'Sm', 'Yb'), ('Ce', 'Sm', 'Lu'), ('Ce', 'Eu', 'Gd'), ('Ce', 'Eu', 'Tb'), ('Ce', 'Eu', 'Dy'), ('Ce', 'Eu', 'Ho'), ('Ce', 'Eu', 'Er '), ('Ce', 'Eu', 'Tm'), ('Ce', 'Eu', 'Yb'), ('Ce', 'Eu', 'Lu'), ('Ce', 'Gd', 'Tb'), ('Ce', 'Gd', 'Dy'), ('Ce', 'Gd', 'Ho'), ('Ce', 'Gd', 'Er'), ('Ce', 'Gd', 'Tm'), ('Ce', 'Gd', 'Yb'), ('Ce', 'Gd', 'Lu'), ('Ce', 'Tb', 'Dy'), ('Ce', ' Tb', 'Ho'), ('Ce', 'Tb', 'Er'), ('Ce', 'Tb', 'Tm'), ('Ce', 'Tb', 'Yb'), ('Ce', 'Tb', 'Lu'), ('Ce', 'Dy', 'Ho'), ('C e', 'Dy', 'Er'), ('Ce', 'Dy', 'Tm'), ('Ce', 'Dy', 'Yb'), ('Ce', 'Dy', 'Lu'), ('Ce', 'Ho', 'Er'), ('Ce', 'Ho', 'Tm'), ('Ce', 'Ho', 'Yb'), ('Ce', 'Ho', 'Lu'), ('Ce', 'Er', 'Tm'), ('Ce', 'Er', 'Yb'), ('Ce', 'Er', 'Lu'), ('Ce', 'Tm', ' Yb'), ('Ce', 'Tm', 'Lu'), ('Ce', 'Yb', 'Lu'), ('Pr', 'Nd', 'Sm'), ('Pr', 'Nd', 'Eu'), ('Pr', 'Nd', 'Gd'), ('Pr', 'N d', 'Tb'), ('Pr', 'Nd', 'Dy'), ('Pr', 'Nd', 'Ho'), ('Pr', 'Nd', 'Er'), ('Pr', 'Nd', 'Tm'), ('Pr', 'Nd', 'Yb'), ('Pr', ' Nd', 'Lu'), ('Pr', 'Sm', 'Eu'), ('Pr', 'Sm', 'Gd'), ('Pr', 'Sm', 'Tb'), ('Pr', 'Sm', 'Dy'), ('Pr', 'Sm', 'Ho'), ('Pr ', 'Sm', 'Er'), ('Pr', 'Sm', 'Tm'), ('Pr', 'Sm', 'Yb'), ('Pr', 'Sm', 'Lu'), ('Pr', 'Eu', 'Gd'), ('Pr', 'Eu', 'Tb'), (' Pr', 'Eu', 'Dy'), ('Pr', 'Eu', 'Ho'), ('Pr', 'Eu', 'Er'), ('Pr', 'Eu', 'Tm'), ('Pr', 'Eu', 'Yb'), ('Pr', 'Eu', 'Lu'), (' Pr', 'Gd', 'Tb'), ('Pr', 'Gd', 'Dy'), ('Pr', 'Gd', 'Ho'), ('Pr', 'Gd', 'Er'), ('Pr', 'Gd', 'Tm'), ('Pr', 'Gd', 'Yb'), ('Pr', 'Gd', 'Lu'), ('Pr', 'Tb', 'Dy'), ('Pr', 'Tb', 'Ho'), ('Pr', 'Tb', 'Er'), ('Pr', 'Tb', 'Tm'), ('Pr', 'Tb', 'Yb'), ('Pr', 'Tb', 'Lu'), ('Pr', 'Dy', 'Ho'), ('Pr', 'Dy', 'Er'), ('Pr', 'Dy', 'Tm'), ('Pr', 'Dy', 'Yb'), ('Pr', 'Dy', 'Lu'), ('Pr', 'Ho', 'Er'), ('Pr', 'Ho', 'Tm'), ('Pr', 'Ho', 'Yb'), ('Pr', 'Ho', 'Lu'), ('Pr', 'Er', 'Tm'), ('Pr', 'Er', 'Yb'), ('Pr', 'Er', 'Lu'), ('Pr', 'Tm', 'Yb'), ('Pr', 'Tm', 'Lu'), ('Pr', 'Yb', 'Lu'), ('Nd', 'Sm', 'Eu'), ('Nd', 'Sm', 'Gd '), ('Nd', 'Sm', 'Tb'), ('Nd', 'Sm', 'Dy'), ('Nd', 'Sm', 'Ho'), ('Nd', 'Sm', 'Er'), ('Nd', 'Sm', 'Tm'), ('Nd', ' Sm', 'Yb'), ('Nd', 'Sm', 'Lu'), ('Nd', 'Eu', 'Gd'), ('Nd', 'Eu', 'Tb'), ('Nd', 'Eu', 'Dy'), ('Nd', 'Eu', 'Ho'), (' Nd', 'Eu', 'Er'), ('Nd', 'Eu', 'Tm'), ('Nd', 'Eu', 'Yb'), ('Nd', 'Eu', 'Lu'), ('Nd', 'Gd', 'Tb'), ('Nd', 'Gd', 'D y'), ('Nd', 'Gd', 'Ho'), ('Nd', 'Gd', 'Er'), ('Nd', 'Gd', 'Tm'), ('Nd', 'Gd', 'Yb'), ('Nd', 'Gd', 'Lu'), ('Nd', ' Tb', 'Dy'), ('Nd', 'Tb', 'Ho'), ('Nd', 'Tb', 'Er'), ('Nd', 'Tb', 'Tm'), ('Nd', 'Tb', 'Yb'), ('Nd', 'Tb', 'Lu'), (' Nd', 'Dy', 'Ho'), ('Nd', 'Dy', 'Er'), ('Nd', 'Dy', 'Tm'), ('Nd', 'Dy', 'Yb'), ('Nd', 'Dy', 'Lu'), ('Nd', 'Ho', ' Er'), ('Nd', 'Ho', 'Tm'), ('Nd', 'Ho', 'Yb'), ('Nd', 'Ho', 'Lu'), ('Nd', 'Er', 'Tm'), ('Nd', 'Er', 'Yb'), ('Nd', ' Er', 'Lu'), ('Nd', 'Tm', 'Yb'), ('Nd', 'Tm', 'Lu'), ('Nd', 'Yb', 'Lu'), ('Sm', 'Eu', 'Gd'), ('Sm', 'Eu', 'Tb'), ( 'Sm', 'Eu', 'Dy'), ('Sm', 'Eu', 'Ho'), ('Sm', 'Eu', 'Er'), ('Sm', 'Eu', 'Tm'), ('Sm', 'Eu', 'Yb'), ('Sm', 'Eu', ' Lu'), ('Sm', 'Gd', 'Tb'), ('Sm', 'Gd', 'Dy'), ('Sm', 'Gd', 'Ho'), ('Sm', 'Gd', 'Er'), ('Sm', 'Gd', 'Tm'), ('Sm ', 'Gd', 'Yb'), ('Sm', 'Gd', 'Lu'), ('Sm', 'Tb', 'Dy'), ('Sm', 'Tb', 'Ho'), ('Sm', 'Tb', 'Er'), ('Sm', 'Tb', 'Tm' ), ('Sm', 'Tb', 'Yb'), ('Sm', 'Tb', 'Lu'), ('Sm', 'Dy', 'Ho'), ('Sm', 'Dy', 'Er'), ('Sm', 'Dy', 'Tm'), ('Sm', 'D y', 'Yb'), ('Sm', 'Dy', 'Lu'), ('Sm', 'Ho', 'Er'), ('Sm', 'Ho', 'Tm'), ('Sm', 'Ho', 'Yb'), ('Sm', 'Ho', 'Lu'), (' Sm', 'Er', 'Tm'), ('Sm', 'Er', 'Yb'), ('Sm', 'Er', 'Lu'), ('Sm', 'Tm', 'Yb'), ('Sm', 'Tm', 'Lu'), ('Sm', 'Yb', ' Lu'), ('Eu', 'Gd', 'Tb'), ('Eu', 'Gd', 'Dy'), ('Eu', 'Gd', 'Ho'), ('Eu', 'Gd', 'Er'), ('Eu', 'Gd', 'Tm'), ('Eu', ' Gd', 'Yb'), ('Eu', 'Gd', 'Lu'), ('Eu', 'Tb', 'Dy'), ('Eu', 'Tb', 'Ho'), ('Eu', 'Tb', 'Er'), ('Eu', 'Tb', 'Tm'), ('E u', 'Tb', 'Yb'), ('Eu', 'Tb', 'Lu'), ('Eu', 'Dy', 'Ho'), ('Eu', 'Dy', 'Er'), ('Eu', 'Dy', 'Tm'), ('Eu', 'Dy', 'Yb'), ('Eu', 'Dy', 'Lu'), ('Eu', 'Ho', 'Er'), ('Eu', 'Ho', 'Tm'), ('Eu', 'Ho', 'Yb'), ('Eu', 'Ho', 'Lu'), ('Eu', 'Er', 'T m'), ('Eu', 'Er', 'Yb'), ('Eu', 'Er', 'Lu'), ('Eu', 'Tm', 'Yb'), ('Eu', 'Tm', 'Lu'), ('Eu', 'Yb', 'Lu'), ('Gd', 'Tb ', 'Dy'), ('Gd', 'Tb', 'Ho'), ('Gd', 'Tb', 'Er'), ('Gd', 'Tb', 'Tm'), ('Gd', 'Tb', 'Yb'), ('Gd', 'Tb', 'Lu'), ('Gd', 'Dy', 'Ho'), ('Gd', 'Dy', 'Er'), ('Gd', 'Dy', 'Tm'), ('Gd', 'Dy', 'Yb'), ('Gd', 'Dy', 'Lu'), ('Gd', 'Ho', 'Er'), ('Gd', 'Ho', 'Tm'), ('Gd', 'Ho', 'Yb'), ('Gd', 'Ho', 'Lu'), ('Gd', 'Er', 'Tm'), ('Gd', 'Er', 'Yb'), ('Gd', 'Er', ' Lu'), ('Gd', 'Tm', 'Yb'), ('Gd', 'Tm', 'Lu'), ('Gd', 'Yb', 'Lu'), ('Tb', 'Dy', 'Ho'), ('Tb', 'Dy', 'Er'), ('Tb', ' Dy', 'Tm'), ('Tb', 'Dy', 'Yb'), ('Tb', 'Dy', 'Lu'), ('Tb', 'Ho', 'Er'), ('Tb', 'Ho', 'Tm'), ('Tb', 'Ho', 'Yb'), (' Tb', 'Ho', 'Lu'), ('Tb', 'Er', 'Tm'), ('Tb', 'Er', 'Yb'), ('Tb', 'Er', 'Lu'), ('Tb', 'Tm', 'Yb'), ('Tb', 'Tm', 'Lu' ), ('Tb', 'Yb', 'Lu'), ('Dy', 'Ho', 'Er'), ('Dy', 'Ho', 'Tm'), ('Dy', 'Ho', 'Yb'), ('Dy', 'Ho', 'Lu'), ('Dy', 'Er', 'Tm'), ('Dy', 'Er', 'Yb'), ('Dy', 'Er', 'Lu'), ('Dy', 'Tm', 'Yb'), ('Dy', 'Tm', 'Lu'), ('Dy', 'Yb', 'Lu'), ('Ho', 'Er', 'Tm'), ('Ho', 'Er', 'Yb'), ('Ho', 'Er', 'Lu'), ('Ho', 'Tm', 'Yb'), ('Ho', 'Tm', 'Lu'), ('Ho', 'Yb', 'Lu'), (' Er', 'Tm', 'Yb'), ('Er', 'Tm', 'Lu'), ('Er', 'Yb', 'Lu'), ('Tm', 'Yb', 'Lu') 3. Example Verification methodology 3: this methodology expands on Verification methodology 2 by the use of naturally occurring microbial cation exchangers, including bacteria and fungi.i. As above but right before step vii (unsealing samples in laboratory), add the following steps:\| ii. Lyse the microbes. For example, autoclave each sample-containing beaker for steam sterilization at 250 °F at 15 psi for 15 minutes. This may lyse any microbes and cause an active release of bio-adsorbed metals.\| iii. Let sample-containing beakers cool to room temperature before proceeding.\| iv. The filter in step (ix) may now act to additionally remove any larger aggregates of microbial cell suspensions that did not lyse in the autoclaving process.\| v. The added EDTA in step (x) in Verification Methodology 2 may act to additionally chelate any REEs that are complexed to the cell wall or organic molecules of the microbial genetic material (as a result of cell lysis).\| vi. In conjunction, verification methodology 3 provides a protocol to achieve full recovery of REEs that were retained in the top 10 cm of soil due to the following biogeochemical processes:1. Mineral surface interface complexation.\| 2. The cation exchange capacity inherent to soils due to organic matter.\| 3. Microbially mediated surface biosorption and/or active biological absorption pathways including but not limited to REE-aqueous complexation with internal genetic material of individual microbial cells found in natural soils and sediments. B. Example systems and methods to enhance the agronomic performance and ecosystem co-benefits:In these non-limiting embodiments, product formulations are detailed that improve the soil quality for improved agronomic applications as well as embodiments that specify improvements on crop health and an ability for plants to protect themselves from pathogens.\| Addition of macronutrients that enhance the agronomic benefits of the applied mineral. Example: addition of elemental 1-5% by weight formulation K or Ca or inexpensive REE such as La to improve use cases of pulverized Mg2SiO4 by improving the nutrient balance of the soil to match the needs of actively growing plants. Application rates for K and Ca may range from 50-100 ppm and lanthanide addition rates may range from 1-50 ppm.\| The 1-5% by volume addition of slow-release acidifiers in the form of elements that maintain the acidity of the soil despite the tendency of the applied mineral to reduce soil acidity in the weathering process. Example: addition of minerals with Al (such as gibbsite, Al(OH)3) or S (such as gypsum, CaSO4)-2H2O), in a rate of 1-10% by weight of total formulation, which contribute to maintaining soil acidity, and thus maintain high rates of weathering, which counteracts the tendency of forsterite weathering to increase alkalinity, which slows rates of weathering.\| The incorporation of additional micronutrients such as zinc (1-5% by weight compared to mineral amendment) to reduce ecosystem losses of phosphorus and downstream ecosystem impacts of phosphate-based fertilizers, such as eutrophication. Phosphates are immobilized via precipitation reactions with the additional zinc metal, so zinc addition slows the transport and reduces mobility of phosphate in the subsoil. As a consequence, phosphate-based fertilizer applications can be performed more safely and with higher confidence that downstream waterways will not form algal blooms and lead to anoxic, uninhabitable waterways for aquatic life. The addition of 1-32 tons/hectare of mineral in conjunction with 1-5% by weight zinc in fields with heavy phosphate application reduces the likelihood of significant phosphate leaching. This also increases nutrient use efficiency, which reduces fertilizer cost to farmers and reduces negative environmental impacts to society. Specifically, phosphate-zinc precipitates become slow-releasing over time due to their immobilization in the soil as a solid phase. This provides longer timeframes for plants to access the phosphate application, reducing the frequency of fertilization.\| The method of mixing of different mineral adjuvants to the primary mineral used for carbon removal can be varied, with impacts on performance. In some embodiments, the admixture (e.g., of gypsum and forsterite) could be completely emulsified. In some embodiments, a nutrient, such as urea, could represent a core that is subsequently coated with a shell of silicate mineral used for carbon removal. In some embodiments the silicate mineral could be the core, and the nutrient, such as urea, could be the coating. In each of these cases, the embodiment can be optimized so as to reduce environmental losses of the nutrient, and increase availability to the plant, while providing the acidity necessary for the silicate mineral weathering. In some embodiments, this may represent a "slow release" nutrient that does not mineralize too quickly and is synchronized more favorably with plant demand.\| Comminution, or pulverization, may help reproduce the expected kinetics of alkalizers such as pulverized limestone or dolomite, known as aglime. Aglime has well-characterized kinetics originating in the particle size distribution of the product, which are in some jurisdictions legally regulated to meet certain requirements. A representative cross section of dissolution kinetics based on actual aglime mesh size observations is depicted in FIG. 2.\|It naturally follows that agronomic performance expectations for silicate minerals used for ERW should follow similar reaction kinetics, particularly in the first year after application, while also meeting the goals for CDR. Thus, an ideal particle size distribution may be tuned to meet this goal. The following shows the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um, such as 90um, which closely approximates the alkalinity release dynamics for aglime.\| The small particle sizes produced by pulverization as above are valuable for performance as an aglime substitute and CDR mechanism, but introduce their own set of potential challenges. One potential challenge is that small particle sizes may fall within regulated categories such as PM10 or PM2.5; another potential challenge is the product may not be easily transferred from one vessel to another (so-called "flowability") because it has a tendency to settle into a compact mass; the product may also not be applied uniformly by extant farm equipment; potentially low uniformity application impacts the agronomic performance as well as the sampling density needed for carbon removal verification. In one potential formulation, the product is pelletized after pulverization, using a common binder such as lignosulfate in a 3-5% ratio by weight of the total formulation. The amount of binder may be optimized to improve performance characteristics during transport and application, but minimize the water and energy needed to dissolve the pellet once it is in the field. Pelletizing the product, into a size range of, for example, 0.5 mm to 3 mm increases the flowability; reduces the prevalence of dust, including the risk of asbestos exposure; enables the use of extant crop input application equipment; and improves the evenness of field distribution, which has the agronomic and carbon verification benefits identified. Pelletizing in this size range also ensures that an adequate number of pellets fall onto any land area which may subsequently be sampled for analysis.\| A desiccated but living biological compound, such as a mycorrhizal inoculum, may be used to coat the agglomerated and dried pellets, so as to enhance the dissolution of the pellet itself after application. This may be distinct from a fungal adjuvant to the pellet to increase dissolution of the silicate minerals themselves.\| To accommodate a range of soil types from acidic to neutral pH, the product may be differentiated into different particle size distributions so as to achieve a consistent rate of weathering across different soil types. For example a consistent rate of weathering may be that the entire applied amount of mineral product weathers in 9 months, allowing a subsequent application every year. To achieve this, an acidic soil may have pellets that contain particles with a modal size on the order of 100 um, while a neutral soil may have pellets that contain particles with a modal size on the order of 10 um. The negative consequence of applying a fine particle in an acidic soil may be that it dissolves too quickly, swinging the pH of the soil too quickly, and altering the nutrient availability severely in the growing plant. The negative consequence of applying a coarse particle in a neutral soil may be that the particle weathers too slowly or is functionally inert, which does not remove carbon as intended, and may subject the farmer or the vendor to risk of clawbacks for payments received for carbon removal. C. Example systems and methods to control or enhance the performance as a securitized carbon removal method:In these non-limiting embodiments, product formulations are described that improve the marketability of pulverized and optionally pelletized mineral amendments as a verifiable carbon removal method, irrespective of their impact on agronomic performance. Such changes in marketability increase the value of the carbon product, for example for detecting and preventing fraud, or increase the dissolution rate (mass per area per year) to accelerate the timing of reapplication, which raises the value in a discounted cash flow analysis. The general scheme is depicted in FIG. 4.\| The addition of low cost and inert trace elements, for example 1-5 ppm neodymium or lanthanum, to a mineral amendment, beyond the natural abundances present in the ore body, improves performance in Verification methods 2 and 3. Specifically, the additional elements reduce measurement uncertainty owing to low natural abundance calculations as well as uncertainty owing to variability from the source mineral. Reduction of these uncertainties improves the detectability of true positives and true negatives. This principle could be applied to many potential soil amendments and fertilizers to verify provenance as pertains to legal contracts.\| The addition of binders to create aggregations of the ground mineral that could reduce drift, which improves distribution uniformity; reduces potential respiratory health impacts; and/or improves applicability of the applied mineral using commercially available equipment. For example, a biofilm mediating organic compound, such as alginate or chitosan, could be mixed with a pulverized mineral with a particle size of approximately 100 microns to achieve an aggregated pellet size of 1 millimeter. This would maintain the advantages of fine particle size, particularly the high specific surface area (m2/g) that mediates dissolution rate, while offsetting potential limitations outlined above. An example methodology for aggregating ground minerals could include these steps:∘ Dissolve 10 grams of alginate powder into solution to create a 0.5 M - 1.0 M alginic acid solution.\| ∘ Heat solution to 80-100 °F to dissolve alginate powder fully if necessary.\| ∘ Spray aerosol sized particles of dissolved alginate powder onto the ground rock material in order to create a biofilm-coated rock material. Apply a consistent spray of 100 mL for each 100 gram of rock (1:1 v/w).\| ∘ The resulting aggregates may have increased bulk density as well as higher aggregating properties due to van der Waals force attraction between the individual rock particles. Dissolution rates can be modified by non-living organic molecules applied concurrently with the mineral amendment. For example, protonated microbes such as acid-treated Arthrobacter nicotianae can constitute an initial release of protons to attack the ground rock materials' crystal structure. This method of acidification for optimal accelerated weathering of rock material may occur even during winter/cold climate. Because biologically mediated processes can have sharp thresholds, e.g., under freezing conditions, such a chemically controlled process would exhibit greater ability to expedite rock breakdown over a range of environmental conditions. To implement this methodology, we outline the following steps:1) De-frost an aliquot of A. nicotianae in 5 mL of Luria broth for about 24 hours at exactly 30 °C.\| 2) Sub-culture into a larger volume of Luria broth at a 1:50 dilution and allow growth for another 24 hours at 30 °C.\| 3) During growth steps #1 and 2, cultures may be shaken, for example at 200-220 RPM, for aeration.\| 4) After culture has been grown for 48 hours in total, centrifuge the cell suspension.\| 5) Collect cell pellet and take a small amount and set it aside. Weigh wet weight, dry at 60 °C overnight, and weigh dry amount to obtain wet : dry conversion.\| 6) Develop an OD600 to wet weight to dry weight conversion by taking 5 varying amounts of wet aliquots of wet biomass and measuring optical density given its known wet mass. Wet aliquots may have a mass of about 1, 4, 8, 12, 16 wet grams and be suspended in 100 mL of DI water.\| 7) Wash cells in 0.1 M NaCl solution.a. Centrifuge cells+growth media at 4000xg.\| b. Carefully pour out LB broth.\| c. Add 0.1 M NaCl solution.\| d. Centrifuge cells+NaCl solution at 4000xg.\| e. Carefully pour out NaCl solution. 8) Protonate the cells while wet.a. Re-suspend the wet biomass in an acidic (e.g., pH 3.0) solution using a dilute hydrochloric acid solution (0.001-0.01 M).\| b. Centrifuge cells+HCl solution at 4000xg.\| c. Carefully pour out solution.\| d. Repeat steps (a)-(c) a total of three times.\| e. Dry cells in an oven at 80-100 °C for 48 hours.\| f. Grind cells using a mortar/pestle to achieve a powder form. 9) Mix 5% w/w of dry cell powder with the ground rock material.\| 10) When this particular rock material+cell powder mixture is applied to agricultural soils, the irrigation or rainfall will re-apply moisture and allow the pre-protonated, re-wet biomass to release their protons. This will ultimately induce a local acidity effect on the rock particle (molecular) level to accelerate rock crystal lattice breakdown. The cells act as biodegradable transporters that are also benign to the natural soil environment.	(EP4256520)\|Cross Reference to Related Applications\|[0001] The present applications claims the priority benefit of U.S. Provisional Patent App. Serial No. 63/322,672, filed March 23, 2022; U.S. Provisional Patent App. Serial No. 63/289,395, filed December 14, 2021; and U.S. Provisional Patent App. Serial No. 63/213,398, filed, June 22, 2021.\|Background\|[0002] The last several years have witnessed a maturation of carbon markets from lightly scrutinized voluntary markets largely serving to provide positive marketing collateral to familiar consumer brands to rigorous compliance markets with proof-of-performance requirements often involving government and quasi-governmental regulators. There have also been a number of comprehensive proposals for decarbonization of the entire US economy, combining energy production, transportation, cement production, and agriculture. These proposals have included carbon dioxide removal (CDR) techniques as an essential component of the decarbonization plan, with a supportive ecosystem of science, policy, and project evaluation criteria. Within the diverse scope of decarbonization efforts, including renewable energy, biofuel, nature-based solutions, and more technical CDR techniques like direct air capture (DAC), The Oxford Principles have developed a taxonomy for categorizing diverse decarbonization strategies. This taxonomy distinguishes between avoided emissions (for instance, conversion of fossil fuel power to renewable power) and negative emissions (for instance direct air capture); distinguishes between avoided emissions that require storage (for instance carbon capture from a point source and sequestration into the ground) and those that do not require storage (the conversion to renewable energy); and the duration of the storage if so required (for instance, short lived forest carbon sequestration from delayed harvests versus storage of captured carbon in geological formations).\|[0003] A number of for-profit and non-profit organizations have emerged that employ the Oxford Principles to evaluate proposals, particularly around the rigorous quantification across categories (Table 1). This, in essence, is the scorecard that projects will have to compete on to find acceptance in the industry. All other things equal, cost ends up being the primary driver, but quality is also a key consideration. Thus, historically buyers have been drawn to nature-based solutions that cost between $5-20/tCO2 e (e.g., Corteva Carbon, Indigo Carbon), versus direct air capture projects that cost >$500/tCO2 e (e.g., ClimeWorks). However, there are challenges to these nature-based solutions: recently these nature-based solutions have been subject to intense scrutiny for "gaming" the rules or otherwise failing to deliver prospective rewards. Among the technological solutions, there are a different set of challenges: rigor has been strong, but the reduction in price proportional to increase in deployment has been slow, and the ultimate price of DAC is not expected to drop below $150/tCO2e (Keith et al 2018, https://doi.org/10.1016/j.joule.2018.05.006). In light of these challenges, we have developed a technology around "enhanced rock weathering" (ERW), in which silicate minerals are weathered in acidic soil solution, thus driving the uptake of additional CO2 into dissolved inorganic carbon (DIC) in the soil solution. Our experimental work, life cycle analysis, and techno-economic modeling have indicated that ERW provides the permanence, additionality, and rigorous quantification of a DAC project, the large volume of a carbon capture and storage (CCS) project, and the unit economics of a nature based solution, thus creating a new tool to meet net-zero goals.\|Details of Enhanced Rock Weathering\|[0004] In "enhanced rock weathering" (ERW), silicate minerals are weathered by CO2 from the ambient air which has been dissolved into water, reacting to produce dissolved inorganic carbon that is ultimately stored in the ocean as depicted in FIGS. 1 and 2.\|Background Geochemistry\|[0005] The role of silicate rock weathering in maintaining the CO2 balance of the atmosphere has been recognized for decades, first outlined by renowned chemist Harold Urey in the 1950s. The basic premise of the Urey reaction is that continental collisions release CO2 to the atmosphere from volcanoes, and bring Mg- and Ca-bearing silicate rocks to the surface. The rainwater (H2O) that falls upon these rocks is mildly acidic, as atmospheric CO2 has dissolved in it and formed carbonic acid (H2CO3). For forsterite, the weathering reaction takes place following the form:\| Mg2SiO4 + 4 H2O + 4 CO2 → 2 Mg2+ + 4 HCO3- + 4 H4SiO4\|[0006] In this reaction, one mole of forsterite consumes four moles of CO2, so two negatively charged bicarbonate HCO3- are created for every one divalent Mg2+ weathered. Given the molecular weight of forsterite (140 g/mol) and the molecular weight of CO2 (44 g/mol), weathering one metric ton of forsterite removes 1.25 metric tons of CO2 from the atmosphere. In general, such a formula can be used to define the "mineral potential" of a silicate based on its elemental composition: \| where V is the valence of the cation (2 for Mg and Ca) and MW is the molecular weight.\|[0007] The rate of weathering is determined by the surface area of the mineral, the acidity (pH) of the soil solution, the temperature of the solution, the availability of CO2 reagent in solution, and the rate of removal of the reaction products by water. One of the key insights into the potential of "enhanced" rock weathering is that the rate of reaction, and thus CO2 removal, can be greatly accelerated by increasing the surface area by pulverization into a fine powder (e.g., less than 100 um), incorporating into an acidic environment (e.g., pH less than 6) with abundant CO2 present, and with steady water flux to remove reaction products to maintain acidity. While this formula defines the potential amount of CO2 that may be removed by weathering, it does not speak to the rate; ancient rock formations testify that the rate of weathering can be extremely slow.\|[0008] The relationship between silicates (like Mg2SiO4) and dissolved carbonates (like HCO3-) is not necessarily intuitive, as the carbonate system of water involves a number of coupled reactions. Atmospheric CO2 dissolves into water according to an exchange coefficient:\| CO2(aq) = H2CO3 = KCO2 * pCO2\|[0009] Technically pCO2 is "fugacity" that represents its activity, but, as used herein, it is more or less equivalent to its partial pressure, and KCO2 is the Henry's law coefficient that determines the aqueous CO2 in equilibrium with the atmosphere. This aqueous CO2 in turn hydrates with H2O to become carbonic acid (H2CO3), which dissociates to become bicarbonate (HCO3-) and carbonate (CO32-):\| H2CO3 ↔ HCO3- + H+\| HCO3- ↔ CO32- + H+\|[0010] These equilibrium reactions are defined by K1 and K2, the first and second carbonate system dissociation constants. pK1 and pK2 are about 5.9 and about 9.4 at STP, so greater than 99% of the charge in the dissolved carbonates is HCO3-.\|[0011] The carbonates are the largest constituents of total alkalinity, which is defined as the charge imbalance between weak acids (proton acceptors) minus proton donors:\| TA = [HCO3-] + 2 · [CO32-] + [OH-] - [H+]\|[0012] There is an alternative definition of total alkalinity as the charge imbalance between conserved cations and conserved anions:\| TA = [Na+] + 2 [Mg2+] + 2 [Ca2+] + [K+] + ... - [Cl-] - 2 [SO42-] - [NO3-]\|[0013] These two expressions are always equal (i.e. the charges balance). This means that an added Mg or Ca into soil solution will increase in HCO3- to balance the charge. We describe an analytical solution to compute how much carbon is taken up per unit of additional Mg or Ca. If we first define DIC as the sum of H2CO3, HCO3-, and CO32-, and make use of the equilibrium equations above (defining H+ as "h" and H2CO3 as "s"): \|[0014] And formulate TA using the same convention: \|[0015] With these definitions in place, we can develop an estimate of dDIC/dTA. First, we compute the derivative dTA/dh: \|[0016] Next we compute the derivative dDIC/dh: \|[0017] Finally we multiply dDIC/dh by the inverse of dTA/dh to calculate dDIC/dTA: \|[0018] At the pH found in soils, each Mg or Ca is matched by two carbon atoms. In all circumstances, raising alkalinity results in increased pH. This is particularly important in marine settings, where ocean acidification from increased atmospheric CO2 can be ameliorated by this export of alkalinity from land.\|[0019] The potential for ERW as a commercial enterprise is limited by some fundamental issues:\| A. The total amounts of mineral transformation and carbon removal should be verifiable empirically. The verification methods described below may be low cost at scale, can be performed at arm's length by a 3rd party, and may have safeguards to eliminate fraud.\|[0020] Additionally, the commercial potential for ERW could be enhanced by a number of different features. Embodiments may include:\| B. Processes and modifications of the engineered mineral product that enhance the agronomic performance and ecosystem co-benefits of the engineered mineral.\| C. Processes and modifications of the engineered mineral product that control or enhance the mineral dissolution rate of the engineered mineral in soil environments and thus the rate of removal of CO2.\| C. Paulo et al, Applied Geochemistry, 2021, 219, 104955, discusses evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralisation.\| N. Moosdorf et al, Environ. Sci. Tech., 2014, 48, 4809 discusses carbon dioxide efficiency of terrestrial enhanced weathering and determination of effective carbon dioxide sequestration.\|Brief Description of the Drawings\|[0021] FIG. 1 is a drawing illustrating the enhanced rock weathering cycle.\| FIG. 2 is a graph depicting the effect of comminution on dissolution kinetics for a silicate.\| FIGS. 3A to 3D are graphs depicting the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um which closely approximates the alkalinity release dynamics for aglime.\| FIG. 4 is a drawing illustrating the general scheme for a verified enhanced rock weathering cycle.\|Detailed Description\|[0022] Summary: The following described methodologies can establish one version of a verification scheme that will demonstrate the transformation of the applied rock material and the subsequent carbon removal into secure geologic reservoirs as evidenced by observations collected from the soil. One set of methods (A) can measure the production of free ions from the applied material and the transport of those ions outside of a control volume as a direct measure of the amount of weathering and thus total carbon dioxide equivalent isolated from the atmosphere. Furthermore, as the elemental inputs into the soil induced by enhanced rock weathering can have significant effects on the soil geochemistry, methods in (B) describe systems and versions that can enhance the agronomic performance of the soil amendment and increase ecosystem co-benefits. Lastly, methods in (C) elaborate on versions that control and enhance the mineral dissolution rate, which increases the financial performance of enhanced rock weathering technology in the marketplace.\| A. Systems and methods for monitoring and verification:Described below are several example methodologies for quantifying the rate and extent of mineral transformation and carbon removal, which are referred to as "verification methodologies".1. Example Verification methodology 1:a. A cation exchange resin and/or an anion exchange resin are packaged into a physical embodiment (such as a 5 cm diameter tube, 5cm in length, placed 30 cm below the soil surface) that allows vertical transport of fluids but not horizontal transport.\| b. Commercial ion exchange resins are pre-equilibrated in such a way that their selectivity is high for the relevant ions, but their capacity is also sufficiently high such that saturation is minimized. This technology may allow for effective deployment for long periods of time, allowing passage of up to 4000 mm of moisture through the tube, without becoming saturated with respect to the ions of interest.\| c. The ions of interest are restricted to divalent cations (Mg2+, Ca2+), carbonate species (HCO3- and CO32-), and silicic acid (H4SiO4), important weathering products of preferred mineral soil amendments, such as ultramafic rocks, blast furnace slag, and other naturally occurring or industrial silicate minerals with high Mg and Ca content.\| d. Three pre-equilibrated tubes are emplaced fully under the soil below a control depth (e.g., 30 cm, a typical depth of cultivation). This may be done by removing the top 30 cm soil with a shovel or auger, then gently placing the tube in the created void space. Following a certain period of time post-surface application of mineral soil amendment (e.g., 9 to 12 months after application), the tubes are retrieved, and the ions captured within the resin exchanges are measured using standard methodologies, such as ICP-OES and ICP-MS based concentration measurements. Three tubes are used to determine standard deviation error in triplicate.\| e. By the principle of charge balance and known thermodynamic reactions taking place in the top 30 cm of soils, the amount of carbonate can be inferred purely from the measurement of cations, under certain assumptions and auxiliary geochemical data. By the addition of more specific anion exchange resins, such as styrenedivinylbenzene, these assumptions can be avoided to get a more precise answer. The increase in cation concentration in the subsurface soil pore water allows for the stoichiometric determination of carbon removal from the gas phase (ambient air).\| f. The total carbon dioxide removed during the deployment period may be estimated as equal to the molecular mass of CO2 (44 g/mol) multiplied by the sum of the number of moles of carbonate and two times the number of moles of bicarbonate, multiplied by the area on which mineral was applied to the field, divided by the cross-sectional area of the tube.\| g. Direct measurement of aqueous bicarbonate and carbonate species, which are the most readily available forms of carbon induced by a gas exchange of carbon dioxide with the soil pore water, may be conducted using the specified anion exchange resin above. The expression as described in clause (f) explains the calculation used to convert this direct measurement of carbon to an absolute value of carbon dioxide removed during a specified application period.\| h. Verification methodology 1 has the advantage that it can provide a direct measure of carbon flux and employs a measurement technique that is mature.\| i. However, potential disadvantages may include the need for manufacturing (and its attendant demand for working capital); devices may occasionally be defective; emplacement of a device may alter the flow paths of water, which in turn alters the inferred ion fluxes; emplacement of a device may depend on the user; the knowledge of the location of emplacement may invite manipulation by a stakeholder involved in a carbon transaction; and others. 2. Example Verification methodology 2:a. The principle behind Verification methodology 2 is that minerals applied for purposes of enhanced rock weathering contain, in addition to the elements outlined above that participate in the weathering reaction (i.e., magnesium, calcium, iron, silicon, oxygen, hydrogen), additional elements in trace amounts. These additional trace elements (TEs) might include rare earth elements (REEs), rare metals (RM), other transition metals (TMs), or a combination thereof. Unlike the primary weathering products that are readily dissolved in solution and lost by leaching, some TEs are strongly bound to mineral and biological surfaces and do not readily leach from the soil control volume (e.g., the top 10 to 30 cm of soil), and are not removed by plants at the concentrations present in our applied rock. These strongly bound trace elements are referred to herein as immobile trace elements (ITEs). Thus, a measure of cumulative cation flux and carbon removal can be computed by comparing the ratio of the lost weathering products, such as magnesium, to ITEs, after accounting for background concentrations of ITEs in the initial soil.\| b. As used herein, rare earth elements include scandium (Sc), yttrium (Y), lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm), europium (Eu), gadolinium (Gd), terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), lutetium (Lu) or a combination thereof. As used herein, rare metals include beryllium (Be), cesium (Cs), gallium (Ga), germanium (Ge), hafnium (Hf), niobium (Nb), rubidium (Rb), tantalum (Ta), zirconium (Zr), or a combination thereof. As used herein, transition metals include nickel (Ni), chromium (Cr), and zinc (Zn) among others and may include a combination of transition metals.\| c. An approach based on ITEs depends on the degree of immobility of the element in soil environments, the time horizon after which the ITEs will be measured to estimate carbon removal, the abundance of ITEs in both the soil and the mineral added, and the analytical chemistry used to measure this abundance. An analytical technique that has low detectability thresholds for slightly mobile elements could be sufficient for relatively abundant (e.g., parts per thousand to parts per million) elements over short time horizons (e.g., weeks to months). On the other hand, a different analytical technique could be used over longer time horizons, which in turn could involve quantification of very immobile elements that are present in much lower abundance (e.g., parts per billion to parts per trillion). The approach may be chosen based at least in part on cost, which ITEs are actually conserved, over which time horizons, as well as the performance of the analytical performance used.\| d. The relative proportions of ITEs in a sample (rock or soil) constitute a type of unique fingerprint of the material. Because the cost of pure ITEs is large, and the analytical chemistry is not widely available, there is a significant barrier to engineering a fraudulent sample to reproduce the native ITE fingerprint of a mineral soil amendment. Thus, it would be challenging for a stakeholder in a carbon exchange transaction to generate a result that produces the anticipated result (a high or low amount of carbon removal) while also matching the ITE fingerprint generated by a bona fide sample. This is a contrast with measurement schemes for soil organic carbon, in which the landowner or other interested party has an information advantage in terms of where or when to sample, which could be used to achieve a particular carbon measurement objective (high or low).\| e. Verification Methodology 2 (VM2) has advantages over Verification Methodology 1 (VM1) in that it avoids the need for the use of a device, which avoids altering the soil hydrology or physical environment in a way that would impact the observed elemental analysis.\| f. VM2 may have an advantage over VM1 in not requiring tracking of a specific location for recovering the sampling column.\| g. VM2 does, however, include measurement techniques that are less widely available; requires specialized instruments and personnel; requires additional boundary conditions to compute carbon flux (e.g., pre-application soil and rock elemental analysis); and employs assumptions as to the relationship between cation flux and carbon flux.\| h. Like VM1, VM2 uses the total amount of mineral applied and the field area, which could be measured, for example, using a digital as-applied map commonly accompanying crops input machinery, or truck weights before and after mineral delivery. This will be referred to as the nominal application rate (ARnominal).\| i. There are four main calculations in VM2. To the extent any one of these factors is known unambiguously from other sources, each step in VM2 could be used in isolation from the others.i. Classify, using ITE fingerprinting, whether a soil has had a specific mineral applied, which may be asserted by an entity wishing to make a claim;\| ii. Calculate, using ITE fingerprinting, what the actual mineral application rate (ARactual) for a specific soil sample was, which will necessarily differ in a systematic or random way from the average rate for the entire field;\| iii. Calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the application rate in (ii) above;\| iv. Calculate, using the fraction computed in (iii) and the mineral potential (Equation 1) computed for the feedstock identified in (i) above, the amount of carbon dioxide removed. j. In one non-limiting embodiment, the verification methodology to classify whether the claimed mineral applied is the actual mineral applied is as follows:i. Collect a sample from mineral to be applied, place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Mineral Amendment.\| ii. Prior to mineral application, collect a 20 g sample from cultivated zone of soil (typically at around 30 cm, such as in a range of 0 cm to 30 cm), place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Soil A.\| iii. Subsequent to mineral application, collect a 20 g sample the same control zone as soil A, and store under similar conditions. Label as Soil B. Soil B could be sampled immediately after mineral application or at a later time (e.g., months to years afterwards).\| iv. Characterize the elemental composition of Mineral Amendment, Soil A, and Soil B. Example approaches to characterizing the elemental composition are described in (v) and (vi).\| v. One approach to measuring the elemental composition is as follows:1. In a laboratory setting, unseal the soil samples and place 10 grams of Soil A and Soil B in two separate beakers.\| 2. Dissolve the solids in strong acid. For example, add 21 mL of strong 1.0 M hydrochloric acid and 7 mL of strong 1.0 M nitric acid (total 28 mL acid) to each beaker of sterilized soil and stir rigorously until solids are dissolved.\| 3. Filter the sample-containing beakers first through a 1- to 5-micron water filter cartridge followed by an attached 10 to 20 cm column cation exchange resin at a sufficiently slow flow rate of, for example, 1 to 5 mL/min. This combination of a water filter with a cation exchange column has been engineered for optimal performance with soils under consideration. Specifically, the 5-micron water filter cartridge separates out any larger particles, allowing for the smaller particles to exchange its bound metals with the subsequent cation exchange resin.\| 4. Flush copious amounts (e.g., 100-200 mL) of 0.5 to 1.0 M chelator such as, for example, ethylenediaminetetraacetic acid (EDTA) at 1-5 mL/min through the used filters into their respective filtrates. This may collect any additional metals that were still adhered to the filters.\| 5. Send filtrate A (resultant sample from Soil A) and filtrate B (resultant sample from Soil B) to an analytical laboratory for analysis on an inductively coupled plasma mass spectrometer (ICP-MS). Measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3.\| 6. The ICP-MS may be set to detect magnesium concentrations and the following 17 elements on a high ppb or low ppm detection level: Yttrium, Scandium, Lanthanum, Cerium, Praseodymium, Neodymium, Promethium, Samarium, Europium, Gadolinium, Terbium, Dysprosium, Holmium, Erbium, Thulium, Ytterbium, Lutetium. Classify light rare earth elements (LREEs) as yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium. Classify heavy rare earth elements (HREEs) as europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium. Send an isolated rock material sample for ICP-MS analysis. Similar to the filtrate analyses, measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3. vi. Another approach to measuring the elemental composition is as follows:1. Calibrate a portable XRF instrument for particularly low detection limit of ITEs using a calibration standard (such as Bruker proprietary Geo calibration + custom ITE standards).\| 2. Use the portable XRF instrument to analyze the Rock Material and Soil A for ITEs (as identified in Verification methodology 2), reporting the instrumental error (2 standard deviations) as well.\| 3. Use the portable XRF instrument to analyze Soil B for ITEs, reporting the instrumental error (2 standard deviations) as well. vii. Once the above elemental composition has been determined, calculate the difference for every element between Mineral Amendment and Soil A, resulting in a vector of differences vrock. Likewise, compute the difference for every element between Soil B and Soil A, resulting in a vector of differences vsoil. To improve performance, each element may be divided by an individual factor, such as the detection threshold, or the instrumental uncertainty, or the elemental composition of a reference material. Another means to improve performance would be to sum a subset of the elements or several distinct subsets of elements before computing vrock and vsoil. Another means to improve performance would be to compute indices of these summed subsets of elements, for example the ratio of the light REEs to the heavy REEs, before computing vrock and vsoil.\| viii. Compute the dot product of vrock and vsoil. If the value of this dot product is close to 1 (e.g., within a threshold value), then the Soil B is positively classified as having the Mineral Amendment. If the value of the dot product is less than 1 minus a threshold value, then Soil B is negatively classified as not having the Mineral Amendment.\| ix. The threshold value may be determined using a variety of means, for example the half-angle between the dot product of vrock and vsoil and any other known vrock and vsoil; or using a Monte Carlo simulation of vrock and vsoil that accounts for known sources of uncertainty including instrumental error, variation in rock elemental analysis, or variation of soil elemental analysis. k. In one non-limiting embodiment, the verification methodology to calculate the actual mineral application rate (ARactual) for a specific soil sample is as follows:i. Characterize the elemental composition the elemental composition of Mineral Amendment, Soil A, and Soil B as above. Note that there could be different analytical chemistry employed if, for example, rapid and inexpensive XRF analysis was used for classification soon after application, and slower and more costly ICP analysis may be used to estimate application rates.\| ii. Compute the differences in elemental composition as above, potentially including similar performance enhancements such as normalizing by factors specific to each element, summing across subsets of elements, and computing indices such as the ratio of light REEs to heavy REEs. Such transformed and summed variables for a sample will be referred to generically as ΣITEsample.\| iii. The actual application rate of the sample can be calculated using the following expression: l. In one non-limiting embodiment, the verification methodology to calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the actual mineral application rate (ARactual) as follows:i. The amount of divalent cations applied (DCapplied) can be calculated by the proven identity of the mineral additive and the actual application rate: where divalent cations are generally restricted in this context to Mg and Ca, and Mgmineral and Camineral is the fractional composition of the mineral additive.\| ii. The amount of divalent cations remaining (DCremain) in the soil could be estimated using the same elemental analysis as previously (if, for example, ICP-MS was used), or determined from the same sample using a different analysis (if, for example XRF was used and Mg was not measured).\| iii. The fractional progress of carbon dioxide removal (CDR) can be estimated by the ratio of remaining divalent cations to applied divalent cations: m. In one non-limiting embodiment, the verification methodology to calculate the amount of carbon dioxide removed from the control volume is as follows:i. Assembling MP, fCDR , ARnominal and the land area applied, the total carbon dioxide removal is: n. While Verification Methodology 2 presented herein provides a broad framework for the detection and application of soil-bound ITEs to estimate long-term geologic carbon drawdown, the efficacy of the approach can also be improved through the focus on specific subsets of ITEs. Non-limiting embodiments of such improvements are listed below:i. The ITEs specified in equation 2, e.g., (ΣITEssoil B), may in fact be represented not by the full summation of 17 REEs but instead by the use of only LREEs or the use of only HREEs, as defined in clause xii. Such a calculation would mean the sum of only LREEs in the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium) or the sum of only HREEs in the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium).\| ii. Within the use of only LREEs for the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium), some LREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual LREEs are selected. For example, the subset may include three LREEs. The calculation (equation 2) is conducted for each of the 3 LREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 LREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [yttrium, scandium, lanthanum], [cerium, lanthanum, neodymium], [cerium, neodymium, samarium], [yttrium, cerium, neodymium], [scandium, neodymium, samarium].\| iii. Within the use of only HREEs for the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium), some HREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual HREEs are selected. For example, the subset may include three HREEs. The calculation (equation 2a) is conducted for each of the 3 HREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 HREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [europium, gadolinium, terbium], [europium, terbium, dysprosium], [dysprosium, erbium, ytterbium], [europium, erbium, ytterbium], [europium, dysprosium, erbium].\| iv. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual REEs are selected. For example, the subset may include three REEs Chart 1 represents a non-limiting list of REE triplicates that may enhance the efficacy of this C drawdown calculation.Chart 1. A non-limiting list of 455 REE triplicates that can be used to effectively triangulate a C drawdown estimation\|('Y', 'La', 'Ce'), ('Y', 'La', 'Pr'), ('Y', 'La', 'Nd'), ('Y', 'La', 'Sm'), ('Y', 'La', 'Eu'), ('Y', 'La', 'Gd'), ('Y', 'La', 'Tb'), ('Y', 'La', 'Dy'), ('Y', 'La', 'Ho'), ('Y', 'La', 'Er'), ('Y', 'La', 'Tm'), ('Y', 'La', 'Yb'), ('Y', 'La', 'Lu'), ('Y', 'Ce', 'Pr'), ('Y', 'Ce', 'Nd'), ('Y', 'Ce', 'Sm'), ('Y', 'Ce', 'Eu'), ('Y', 'Ce', 'Gd'), ('Y', 'Ce', 'Tb' ), ('Y', 'Ce', 'Dy'), ('Y', 'Ce', 'Ho'), ('Y', 'Ce', 'Er'), ('Y', 'Ce', 'Tm'), ('Y', 'Ce', 'Yb'), ('Y', 'Ce', 'Lu'), (' Y', 'Pr', 'Nd'), ('Y', 'Pr', 'Sm'), ('Y', 'Pr', 'Eu'), ('Y', 'Pr', 'Gd'), ('Y', 'Pr', 'Tb'), ('Y', 'Pr', 'Dy'), ('Y', 'Pr ', 'Ho'), ('Y', 'Pr', 'Er'), ('Y', 'Pr', 'Tm'), ('Y', 'Pr', 'Yb'), ('Y', 'Pr', 'Lu'), ('Y', 'Nd', 'Sm'), ('Y', 'Nd', 'E u'), ('Y', 'Nd', 'Gd'), ('Y', 'Nd', 'Tb'), ('Y', 'Nd', 'Dy'), ('Y', 'Nd', 'Ho'), ('Y', 'Nd', 'Er'), ('Y', 'Nd', 'Tm' ), ('Y', 'Nd', 'Yb'), ('Y', 'Nd', 'Lu'), ('Y', 'Sm', 'Eu'), ('Y', 'Sm', 'Gd'), ('Y', 'Sm', 'Tb'), ('Y', 'Sm', 'Dy'), ('Y', 'Sm', 'Ho'), ('Y', 'Sm', 'Er'), ('Y', 'Sm', 'Tm'), ('Y', 'Sm', 'Yb'), ('Y', 'Sm', 'Lu'), ('Y', 'Eu', 'Gd'), ('Y', 'Eu', 'Tb'), ('Y', 'Eu', 'Dy'), ('Y', 'Eu', 'Ho'), ('Y', 'Eu', 'Er'), ('Y', 'Eu', 'Tm'), ('Y', 'Eu', 'Yb'), ('Y ', 'Eu', 'Lu'), ('Y', 'Gd', 'Tb'), ('Y', 'Gd', 'Dy'), ('Y', 'Gd', 'Ho'), ('Y', 'Gd', 'Er'), ('Y', 'Gd', 'Tm'), ('Y', ' Gd', 'Yb'), ('Y', 'Gd', 'Lu'), ('Y', 'Tb', 'Dy'), ('Y', 'Tb', 'Ho'), ('Y', 'Tb', 'Er'), ('Y', 'Tb', 'Tm'), ('Y', 'Tb ', 'Yb'), ('Y', 'Tb', 'Lu'), ('Y', 'Dy', 'Ho'), ('Y', 'Dy', 'Er'), ('Y', 'Dy', 'Tm'), ('Y', 'Dy', 'Yb'), ('Y', 'Dy', 'Lu'), ('Y', 'Ho', 'Er'), ('Y', 'Ho', 'Tm'), ('Y', 'Ho', 'Yb'), ('Y', 'Ho', 'Lu'), ('Y', 'Er', 'Tm'), ('Y', 'Er', 'Y b'), ('Y', 'Er', 'Lu'), ('Y', 'Tm', 'Yb'), ('Y', 'Tm', 'Lu'), ('Y', 'Yb', 'Lu'), ('La', 'Ce', 'Pr'), ('La', 'Ce', 'Nd' ), ('La', 'Ce', 'Sm'), ('La', 'Ce', 'Eu'), ('La', 'Ce', 'Gd'), ('La', 'Ce', 'Tb'), ('La', 'Ce', 'Dy'), ('La', 'Ce', ' Ho'), ('La', 'Ce', 'Er'), ('La', 'Ce', 'Tm'), ('La', 'Ce', 'Yb'), ('La', 'Ce', 'Lu'), ('La', 'Pr', 'Nd'), ('La', 'Pr', 'Sm'), ('La', 'Pr', 'Eu'), ('La', 'Pr', 'Gd'), ('La', 'Pr', 'Tb'), ('La', 'Pr', 'Dy'), ('La', 'Pr', 'Ho'), ('La', 'Pr', ' Er'), ('La', 'Pr', 'Tm'), ('La', 'Pr', 'Yb'), ('La', 'Pr', 'Lu'), ('La', 'Nd', 'Sm'), ('La', 'Nd', 'Eu'), ('La', 'Nd', 'Gd'), ('La', 'Nd', 'Tb'), ('La', 'Nd', 'Dy'), ('La', 'Nd', 'Ho'), ('La', 'Nd', 'Er'), ('La', 'Nd', 'Tm'), ('La', ' Nd', 'Yb'), ('La', 'Nd', 'Lu'), ('La', 'Sm', 'Eu'), ('La', 'Sm', 'Gd'), ('La', 'Sm', 'Tb'), ('La', 'Sm', 'Dy'), (' La', 'Sm', 'Ho'), ('La', 'Sm', 'Er'), ('La', 'Sm', 'Tm'), ('La', 'Sm', 'Yb'), ('La', 'Sm', 'Lu'), ('La', 'Eu', 'G d'), ('La', 'Eu', 'Tb'), ('La', 'Eu', 'Dy'), ('La', 'Eu', 'Ho'), ('La', 'Eu', 'Er'), ('La', 'Eu', 'Tm'), ('La', 'Eu', ' Yb'), ('La', 'Eu', 'Lu'), ('La', 'Gd', 'Tb'), ('La', 'Gd', 'Dy'), ('La', 'Gd', 'Ho'), ('La', 'Gd', 'Er'), ('La', 'G d', 'Tm'), ('La', 'Gd', 'Yb'), ('La', 'Gd', 'Lu'), ('La', 'Tb', 'Dy'), ('La', 'Tb', 'Ho'), ('La', 'Tb', 'Er'), ('La', 'Tb', 'Tm'), ('La', 'Tb', 'Yb'), ('La', 'Tb', 'Lu'), ('La', 'Dy', 'Ho'), ('La', 'Dy', 'Er'), ('La', 'Dy', 'Tm'), ('L a', 'Dy', 'Yb'), ('La', 'Dy', 'Lu'), ('La', 'Ho', 'Er'), ('La', 'Ho', 'Tm'), ('La', 'Ho', 'Yb'), ('La', 'Ho', 'Lu'), ('La', 'Er', 'Tm'), ('La', 'Er', 'Yb'), ('La', 'Er', 'Lu'), ('La', 'Tm', 'Yb'), ('La', 'Tm', 'Lu'), ('La', 'Yb', 'Lu' ), ('Ce', 'Pr', 'Nd'), ('Ce', 'Pr', 'Sm'), ('Ce', 'Pr', 'Eu'), ('Ce', 'Pr', 'Gd'), ('Ce', 'Pr', 'Tb'), ('Ce', 'Pr', 'Dy' ), ('Ce', 'Pr', 'Ho'), ('Ce', 'Pr', 'Er'), ('Ce', 'Pr', 'Tm'), ('Ce', 'Pr', 'Yb'), ('Ce', 'Pr', 'Lu'), ('Ce', 'Nd', 'Sm '), ('Ce', 'Nd', 'Eu'), ('Ce', 'Nd', 'Gd'), ('Ce', 'Nd', 'Tb'), ('Ce', 'Nd', 'Dy'), ('Ce', 'Nd', 'Ho'), ('Ce', 'Nd', 'Er'), ('Ce', 'Nd', 'Tm'), ('Ce', 'Nd', 'Yb'), ('Ce', 'Nd', 'Lu'), ('Ce', 'Sm', 'Eu'), ('Ce', 'Sm', 'Gd'), ('Ce', ' Sm', 'Tb'), ('Ce', 'Sm', 'Dy'), ('Ce', 'Sm', 'Ho'), ('Ce', 'Sm', 'Er'), ('Ce', 'Sm', 'Tm'), ('Ce', 'Sm', 'Yb'), ('Ce', 'Sm', 'Lu'), ('Ce', 'Eu', 'Gd'), ('Ce', 'Eu', 'Tb'), ('Ce', 'Eu', 'Dy'), ('Ce', 'Eu', 'Ho'), ('Ce', 'Eu', 'Er '), ('Ce', 'Eu', 'Tm'), ('Ce', 'Eu', 'Yb'), ('Ce', 'Eu', 'Lu'), ('Ce', 'Gd', 'Tb'), ('Ce', 'Gd', 'Dy'), ('Ce', 'Gd', 'Ho'), ('Ce', 'Gd', 'Er'), ('Ce', 'Gd', 'Tm'), ('Ce', 'Gd', 'Yb'), ('Ce', 'Gd', 'Lu'), ('Ce', 'Tb', 'Dy'), ('Ce', ' Tb', 'Ho'), ('Ce', 'Tb', 'Er'), ('Ce', 'Tb', 'Tm'), ('Ce', 'Tb', 'Yb'), ('Ce', 'Tb', 'Lu'), ('Ce', 'Dy', 'Ho'), ('C e', 'Dy', 'Er'), ('Ce', 'Dy', 'Tm'), ('Ce', 'Dy', 'Yb'), ('Ce', 'Dy', 'Lu'), ('Ce', 'Ho', 'Er'), ('Ce', 'Ho', 'Tm'), ('Ce', 'Ho', 'Yb'), ('Ce', 'Ho', 'Lu'), ('Ce', 'Er', 'Tm'), ('Ce', 'Er', 'Yb'), ('Ce', 'Er', 'Lu'), ('Ce', 'Tm', ' Yb'), ('Ce', 'Tm', 'Lu'), ('Ce', 'Yb', 'Lu'), ('Pr', 'Nd', 'Sm'), ('Pr', 'Nd', 'Eu'), ('Pr', 'Nd', 'Gd'), ('Pr', 'N d', 'Tb'), ('Pr', 'Nd', 'Dy'), ('Pr', 'Nd', 'Ho'), ('Pr', 'Nd', 'Er'), ('Pr', 'Nd', 'Tm'), ('Pr', 'Nd', 'Yb'), ('Pr', ' Nd', 'Lu'), ('Pr', 'Sm', 'Eu'), ('Pr', 'Sm', 'Gd'), ('Pr', 'Sm', 'Tb'), ('Pr', 'Sm', 'Dy'), ('Pr', 'Sm', 'Ho'), ('Pr ', 'Sm', 'Er'), ('Pr', 'Sm', 'Tm'), ('Pr', 'Sm', 'Yb'), ('Pr', 'Sm', 'Lu'), ('Pr', 'Eu', 'Gd'), ('Pr', 'Eu', 'Tb'), (' Pr', 'Eu', 'Dy'), ('Pr', 'Eu', 'Ho'), ('Pr', 'Eu', 'Er'), ('Pr', 'Eu', 'Tm'), ('Pr', 'Eu', 'Yb'), ('Pr', 'Eu', 'Lu'), (' Pr', 'Gd', 'Tb'), ('Pr', 'Gd', 'Dy'), ('Pr', 'Gd', 'Ho'), ('Pr', 'Gd', 'Er'), ('Pr', 'Gd', 'Tm'), ('Pr', 'Gd', 'Yb'), ('Pr', 'Gd', 'Lu'), ('Pr', 'Tb', 'Dy'), ('Pr', 'Tb', 'Ho'), ('Pr', 'Tb', 'Er'), ('Pr', 'Tb', 'Tm'), ('Pr', 'Tb', 'Yb'), ('Pr', 'Tb', 'Lu'), ('Pr', 'Dy', 'Ho'), ('Pr', 'Dy', 'Er'), ('Pr', 'Dy', 'Tm'), ('Pr', 'Dy', 'Yb'), ('Pr', 'Dy', 'Lu'), ('Pr', 'Ho', 'Er'), ('Pr', 'Ho', 'Tm'), ('Pr', 'Ho', 'Yb'), ('Pr', 'Ho', 'Lu'), ('Pr', 'Er', 'Tm'), ('Pr', 'Er', 'Yb'), ('Pr', 'Er', 'Lu'), ('Pr', 'Tm', 'Yb'), ('Pr', 'Tm', 'Lu'), ('Pr', 'Yb', 'Lu'), ('Nd', 'Sm', 'Eu'), ('Nd', 'Sm', 'Gd '), ('Nd', 'Sm', 'Tb'), ('Nd', 'Sm', 'Dy'), ('Nd', 'Sm', 'Ho'), ('Nd', 'Sm', 'Er'), ('Nd', 'Sm', 'Tm'), ('Nd', ' Sm', 'Yb'), ('Nd', 'Sm', 'Lu'), ('Nd', 'Eu', 'Gd'), ('Nd', 'Eu', 'Tb'), ('Nd', 'Eu', 'Dy'), ('Nd', 'Eu', 'Ho'), (' Nd', 'Eu', 'Er'), ('Nd', 'Eu', 'Tm'), ('Nd', 'Eu', 'Yb'), ('Nd', 'Eu', 'Lu'), ('Nd', 'Gd', 'Tb'), ('Nd', 'Gd', 'D y'), ('Nd', 'Gd', 'Ho'), ('Nd', 'Gd', 'Er'), ('Nd', 'Gd', 'Tm'), ('Nd', 'Gd', 'Yb'), ('Nd', 'Gd', 'Lu'), ('Nd', ' Tb', 'Dy'), ('Nd', 'Tb', 'Ho'), ('Nd', 'Tb', 'Er'), ('Nd', 'Tb', 'Tm'), ('Nd', 'Tb', 'Yb'), ('Nd', 'Tb', 'Lu'), (' Nd', 'Dy', 'Ho'), ('Nd', 'Dy', 'Er'), ('Nd', 'Dy', 'Tm'), ('Nd', 'Dy', 'Yb'), ('Nd', 'Dy', 'Lu'), ('Nd', 'Ho', ' Er'), ('Nd', 'Ho', 'Tm'), ('Nd', 'Ho', 'Yb'), ('Nd', 'Ho', 'Lu'), ('Nd', 'Er', 'Tm'), ('Nd', 'Er', 'Yb'), ('Nd', ' Er', 'Lu'), ('Nd', 'Tm', 'Yb'), ('Nd', 'Tm', 'Lu'), ('Nd', 'Yb', 'Lu'), ('Sm', 'Eu', 'Gd'), ('Sm', 'Eu', 'Tb'), ( 'Sm', 'Eu', 'Dy'), ('Sm', 'Eu', 'Ho'), ('Sm', 'Eu', 'Er'), ('Sm', 'Eu', 'Tm'), ('Sm', 'Eu', 'Yb'), ('Sm', 'Eu', ' Lu'), ('Sm', 'Gd', 'Tb'), ('Sm', 'Gd', 'Dy'), ('Sm', 'Gd', 'Ho'), ('Sm', 'Gd', 'Er'), ('Sm', 'Gd', 'Tm'), ('Sm ', 'Gd', 'Yb'), ('Sm', 'Gd', 'Lu'), ('Sm', 'Tb', 'Dy'), ('Sm', 'Tb', 'Ho'), ('Sm', 'Tb', 'Er'), ('Sm', 'Tb', 'Tm' ), ('Sm', 'Tb', 'Yb'), ('Sm', 'Tb', 'Lu'), ('Sm', 'Dy', 'Ho'), ('Sm', 'Dy', 'Er'), ('Sm', 'Dy', 'Tm'), ('Sm', 'D y', 'Yb'), ('Sm', 'Dy', 'Lu'), ('Sm', 'Ho', 'Er'), ('Sm', 'Ho', 'Tm'), ('Sm', 'Ho', 'Yb'), ('Sm', 'Ho', 'Lu'), (' Sm', 'Er', 'Tm'), ('Sm', 'Er', 'Yb'), ('Sm', 'Er', 'Lu'), ('Sm', 'Tm', 'Yb'), ('Sm', 'Tm', 'Lu'), ('Sm', 'Yb', ' Lu'), ('Eu', 'Gd', 'Tb'), ('Eu', 'Gd', 'Dy'), ('Eu', 'Gd', 'Ho'), ('Eu', 'Gd', 'Er'), ('Eu', 'Gd', 'Tm'), ('Eu', ' Gd', 'Yb'), ('Eu', 'Gd', 'Lu'), ('Eu', 'Tb', 'Dy'), ('Eu', 'Tb', 'Ho'), ('Eu', 'Tb', 'Er'), ('Eu', 'Tb', 'Tm'), ('E u', 'Tb', 'Yb'), ('Eu', 'Tb', 'Lu'), ('Eu', 'Dy', 'Ho'), ('Eu', 'Dy', 'Er'), ('Eu', 'Dy', 'Tm'), ('Eu', 'Dy', 'Yb'), ('Eu', 'Dy', 'Lu'), ('Eu', 'Ho', 'Er'), ('Eu', 'Ho', 'Tm'), ('Eu', 'Ho', 'Yb'), ('Eu', 'Ho', 'Lu'), ('Eu', 'Er', 'T m'), ('Eu', 'Er', 'Yb'), ('Eu', 'Er', 'Lu'), ('Eu', 'Tm', 'Yb'), ('Eu', 'Tm', 'Lu'), ('Eu', 'Yb', 'Lu'), ('Gd', 'Tb ', 'Dy'), ('Gd', 'Tb', 'Ho'), ('Gd', 'Tb', 'Er'), ('Gd', 'Tb', 'Tm'), ('Gd', 'Tb', 'Yb'), ('Gd', 'Tb', 'Lu'), ('Gd', 'Dy', 'Ho'), ('Gd', 'Dy', 'Er'), ('Gd', 'Dy', 'Tm'), ('Gd', 'Dy', 'Yb'), ('Gd', 'Dy', 'Lu'), ('Gd', 'Ho', 'Er'), ('Gd', 'Ho', 'Tm'), ('Gd', 'Ho', 'Yb'), ('Gd', 'Ho', 'Lu'), ('Gd', 'Er', 'Tm'), ('Gd', 'Er', 'Yb'), ('Gd', 'Er', ' Lu'), ('Gd', 'Tm', 'Yb'), ('Gd', 'Tm', 'Lu'), ('Gd', 'Yb', 'Lu'), ('Tb', 'Dy', 'Ho'), ('Tb', 'Dy', 'Er'), ('Tb', ' Dy', 'Tm'), ('Tb', 'Dy', 'Yb'), ('Tb', 'Dy', 'Lu'), ('Tb', 'Ho', 'Er'), ('Tb', 'Ho', 'Tm'), ('Tb', 'Ho', 'Yb'), (' Tb', 'Ho', 'Lu'), ('Tb', 'Er', 'Tm'), ('Tb', 'Er', 'Yb'), ('Tb', 'Er', 'Lu'), ('Tb', 'Tm', 'Yb'), ('Tb', 'Tm', 'Lu' ), ('Tb', 'Yb', 'Lu'), ('Dy', 'Ho', 'Er'), ('Dy', 'Ho', 'Tm'), ('Dy', 'Ho', 'Yb'), ('Dy', 'Ho', 'Lu'), ('Dy', 'Er', 'Tm'), ('Dy', 'Er', 'Yb'), ('Dy', 'Er', 'Lu'), ('Dy', 'Tm', 'Yb'), ('Dy', 'Tm', 'Lu'), ('Dy', 'Yb', 'Lu'), ('Ho', 'Er', 'Tm'), ('Ho', 'Er', 'Yb'), ('Ho', 'Er', 'Lu'), ('Ho', 'Tm', 'Yb'), ('Ho', 'Tm', 'Lu'), ('Ho', 'Yb', 'Lu'), (' Er', 'Tm', 'Yb'), ('Er', 'Tm', 'Lu'), ('Er', 'Yb', 'Lu'), ('Tm', 'Yb', 'Lu') 3. Example Verification methodology 3: this methodology expands on Verification methodology 2 by the use of naturally occurring microbial cation exchangers, including bacteria and fungi.i. As above but right before step vii (unsealing samples in laboratory), add the following steps:\| ii. Lyse the microbes. For example, autoclave each sample-containing beaker for steam sterilization at 250 °F at 15 psi for 15 minutes. This may lyse any microbes and cause an active release of bio-adsorbed metals.\| iii. Let sample-containing beakers cool to room temperature before proceeding.\| iv. The filter in step (ix) may now act to additionally remove any larger aggregates of microbial cell suspensions that did not lyse in the autoclaving process.\| v. The added EDTA in step (x) in Verification Methodology 2 may act to additionally chelate any REEs that are complexed to the cell wall or organic molecules of the microbial genetic material (as a result of cell lysis).\| vi. In conjunction, verification methodology 3 provides a protocol to achieve full recovery of REEs that were retained in the top 10 cm of soil due to the following biogeochemical processes:1. Mineral surface interface complexation.\| 2. The cation exchange capacity inherent to soils due to organic matter.\| 3. Microbially mediated surface biosorption and/or active biological absorption pathways including but not limited to REE-aqueous complexation with internal genetic material of individual microbial cells found in natural soils and sediments. B. Example systems and methods to enhance the agronomic performance and ecosystem co-benefits:In these non-limiting embodiments, product formulations are detailed that improve the soil quality for improved agronomic applications as well as embodiments that specify improvements on crop health and an ability for plants to protect themselves from pathogens.\| Addition of macronutrients that enhance the agronomic benefits of the applied mineral. Example: addition of elemental 1-5% by weight formulation K or Ca or inexpensive REE such as La to improve use cases of pulverized Mg2SiO4 by improving the nutrient balance of the soil to match the needs of actively growing plants. Application rates for K and Ca may range from 50-100 ppm and lanthanide addition rates may range from 1-50 ppm.\| The 1-5% by volume addition of slow-release acidifiers in the form of elements that maintain the acidity of the soil despite the tendency of the applied mineral to reduce soil acidity in the weathering process. Example: addition of minerals with Al (such as gibbsite, Al(OH)3) or S (such as gypsum, CaSO4)-2H2O), in a rate of 1-10% by weight of total formulation, which contribute to maintaining soil acidity, and thus maintain high rates of weathering, which counteracts the tendency of forsterite weathering to increase alkalinity, which slows rates of weathering.\| The incorporation of additional micronutrients such as zinc (1-5% by weight compared to mineral amendment) to reduce ecosystem losses of phosphorus and downstream ecosystem impacts of phosphate-based fertilizers, such as eutrophication. Phosphates are immobilized via precipitation reactions with the additional zinc metal, so zinc addition slows the transport and reduces mobility of phosphate in the subsoil. As a consequence, phosphate-based fertilizer applications can be performed more safely and with higher confidence that downstream waterways will not form algal blooms and lead to anoxic, uninhabitable waterways for aquatic life. The addition of 1-32 tons/hectare of mineral in conjunction with 1-5% by weight zinc in fields with heavy phosphate application reduces the likelihood of significant phosphate leaching. This also increases nutrient use efficiency, which reduces fertilizer cost to farmers and reduces negative environmental impacts to society. Specifically, phosphate-zinc precipitates become slow-releasing over time due to their immobilization in the soil as a solid phase. This provides longer timeframes for plants to access the phosphate application, reducing the frequency of fertilization.\| The method of mixing of different mineral adjuvants to the primary mineral used for carbon removal can be varied, with impacts on performance. In some embodiments, the admixture (e.g., of gypsum and forsterite) could be completely emulsified. In some embodiments, a nutrient, such as urea, could represent a core that is subsequently coated with a shell of silicate mineral used for carbon removal. In some embodiments the silicate mineral could be the core, and the nutrient, such as urea, could be the coating. In each of these cases, the embodiment can be optimized so as to reduce environmental losses of the nutrient, and increase availability to the plant, while providing the acidity necessary for the silicate mineral weathering. In some embodiments, this may represent a "slow release" nutrient that does not mineralize too quickly and is synchronized more favorably with plant demand.\| Comminution, or pulverization, may help reproduce the expected kinetics of alkalizers such as pulverized limestone or dolomite, known as aglime. Aglime has well-characterized kinetics originating in the particle size distribution of the product, which are in some jurisdictions legally regulated to meet certain requirements. A representative cross section of dissolution kinetics based on actual aglime mesh size observations is depicted in FIG. 2.\|It naturally follows that agronomic performance expectations for silicate minerals used for ERW should follow similar reaction kinetics, particularly in the first year after application, while also meeting the goals for CDR. Thus, an ideal particle size distribution may be tuned to meet this goal. The following shows the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um, such as 90um, which closely approximates the alkalinity release dynamics for aglime.\| The small particle sizes produced by pulverization as above are valuable for performance as an aglime substitute and CDR mechanism, but introduce their own set of potential challenges. One potential challenge is that small particle sizes may fall within regulated categories such as PM10 or PM2.5; another potential challenge is the product may not be easily transferred from one vessel to another (so-called "flowability") because it has a tendency to settle into a compact mass; the product may also not be applied uniformly by extant farm equipment; potentially low uniformity application impacts the agronomic performance as well as the sampling density needed for carbon removal verification. In one potential formulation, the product is pelletized after pulverization, using a common binder such as lignosulfate in a 3-5% ratio by weight of the total formulation. The amount of binder may be optimized to improve performance characteristics during transport and application, but minimize the water and energy needed to dissolve the pellet once it is in the field. Pelletizing the product, into a size range of, for example, 0.5 mm to 3 mm increases the flowability; reduces the prevalence of dust, including the risk of asbestos exposure; enables the use of extant crop input application equipment; and improves the evenness of field distribution, which has the agronomic and carbon verification benefits identified. Pelletizing in this size range also ensures that an adequate number of pellets fall onto any land area which may subsequently be sampled for analysis.\| A desiccated but living biological compound, such as a mycorrhizal inoculum, may be used to coat the agglomerated and dried pellets, so as to enhance the dissolution of the pellet itself after application. This may be distinct from a fungal adjuvant to the pellet to increase dissolution of the silicate minerals themselves.\| To accommodate a range of soil types from acidic to neutral pH, the product may be differentiated into different particle size distributions so as to achieve a consistent rate of weathering across different soil types. For example a consistent rate of weathering may be that the entire applied amount of mineral product weathers in 9 months, allowing a subsequent application every year. To achieve this, an acidic soil may have pellets that contain particles with a modal size on the order of 100 um, while a neutral soil may have pellets that contain particles with a modal size on the order of 10 um. The negative consequence of applying a fine particle in an acidic soil may be that it dissolves too quickly, swinging the pH of the soil too quickly, and altering the nutrient availability severely in the growing plant. The negative consequence of applying a coarse particle in a neutral soil may be that the particle weathers too slowly or is functionally inert, which does not remove carbon as intended, and may subject the farmer or the vendor to risk of clawbacks for payments received for carbon removal. C. Example systems and methods to control or enhance the performance as a securitized carbon removal method:In these non-limiting embodiments, product formulations are described that improve the marketability of pulverized and optionally pelletized mineral amendments as a verifiable carbon removal method, irrespective of their impact on agronomic performance. Such changes in marketability increase the value of the carbon product, for example for detecting and preventing fraud, or increase the dissolution rate (mass per area per year) to accelerate the timing of reapplication, which raises the value in a discounted cash flow analysis. The general scheme is depicted in FIG. 4.\| The addition of low cost and inert trace elements, for example 1-5 ppm neodymium or lanthanum, to a mineral amendment, beyond the natural abundances present in the ore body, improves performance in Verification methods 2 and 3. Specifically, the additional elements reduce measurement uncertainty owing to low natural abundance calculations as well as uncertainty owing to variability from the source mineral. Reduction of these uncertainties improves the detectability of true positives and true negatives. This principle could be applied to many potential soil amendments and fertilizers to verify provenance as pertains to legal contracts.\| The addition of binders to create aggregations of the ground mineral that could reduce drift, which improves distribution uniformity; reduces potential respiratory health impacts; and/or improves applicability of the applied mineral using commercially available equipment. For example, a biofilm mediating organic compound, such as alginate or chitosan, could be mixed with a pulverized mineral with a particle size of approximately 100 microns to achieve an aggregated pellet size of 1 millimeter. This would maintain the advantages of fine particle size, particularly the high specific surface area (m2/g) that mediates dissolution rate, while offsetting potential limitations outlined above. An example methodology for aggregating ground minerals could include these steps:∘ Dissolve 10 grams of alginate powder into solution to create a 0.5 M - 1.0 M alginic acid solution.\| ∘ Heat solution to 80-100 °F to dissolve alginate powder fully if necessary.\| ∘ Spray aerosol sized particles of dissolved alginate powder onto the ground rock material in order to create a biofilm-coated rock material. Apply a consistent spray of 100 mL for each 100 gram of rock (1:1 v/w).\| ∘ The resulting aggregates may have increased bulk density as well as higher aggregating properties due to van der Waals force attraction between the individual rock particles. Dissolution rates can be modified by non-living organic molecules applied concurrently with the mineral amendment. For example, protonated microbes such as acid-treated Arthrobacter nicotianae can constitute an initial release of protons to attack the ground rock materials' crystal structure. This method of acidification for optimal accelerated weathering of rock material may occur even during winter/cold climate. Because biologically mediated processes can have sharp thresholds, e.g., under freezing conditions, such a chemically controlled process would exhibit greater ability to expedite rock breakdown over a range of environmental conditions. To implement this methodology, we outline the following steps:1) De-frost an aliquot of A. nicotianae in 5 mL of Luria broth for about 24 hours at exactly 30 °C.\| 2) Sub-culture into a larger volume of Luria broth at a 1:50 dilution and allow growth for another 24 hours at 30 °C.\| 3) During growth steps #1 and 2, cultures may be shaken, for example at 200-220 RPM, for aeration.\| 4) After culture has been grown for 48 hours in total, centrifuge the cell suspension.\| 5) Collect cell pellet and take a small amount and set it aside. Weigh wet weight, dry at 60 °C overnight, and weigh dry amount to obtain wet : dry conversion.\| 6) Develop an OD600 to wet weight to dry weight conversion by taking 5 varying amounts of wet aliquots of wet biomass and measuring optical density given its known wet mass. Wet aliquots may have a mass of about 1, 4, 8, 12, 16 wet grams and be suspended in 100 mL of DI water.\| 7) Wash cells in 0.1 M NaCl solution.a. Centrifuge cells+growth media at 4000xg.\| b. Carefully pour out LB broth.\| c. Add 0.1 M NaCl solution.\| d. Centrifuge cells+NaCl solution at 4000xg.\| e. Carefully pour out NaCl solution. 8) Protonate the cells while wet.a. Re-suspend the wet biomass in an acidic (e.g., pH 3.0) solution using a dilute hydrochloric acid solution (0.001-0.01 M).\| b. Centrifuge cells+HCl solution at 4000xg.\| c. Carefully pour out solution.\| d. Repeat steps (a)-(c) a total of three times.\| e. Dry cells in an oven at 80-100 °C for 48 hours.\| f. Grind cells using a mortar/pestle to achieve a powder form. 9) Mix 5% w/w of dry cell powder with the ground rock material.\| 10) When this particular rock material+cell powder mixture is applied to agricultural soils, the irrigation or rainfall will re-apply moisture and allow the pre-protonated, re-wet biomass to release their protons. This will ultimately induce a local acidity effect on the rock particle (molecular) level to accelerate rock crystal lattice breakdown. The cells act as biodegradable transporters that are also benign to the natural soil environment.	Family Number\|(103013820)\|103013820\|Object of Invention\|(US11644454 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20220404329 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(WO2022271842 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20230273174 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US11921098 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(EP4276752 A2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(EP4276752 A3)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20240264139 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US12422425 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20260016458 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|Abstract\|(US11644454 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(WO2022271842 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(AU2022299180 A9)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.(From EP4276752 A3)\|(CA3207124 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US11921098 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(EP4256520 C0)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(EP4276752 A3)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(BR112023023226 B1)\|verification methods and agronomic enhancements for carbon removal based on improved weathering of rocks. this description refers to methods to verify improved weathering of rocks using traces of immovable elements found within a mineral correction. mineral corrections that allow for improved weathering of rocks are also described\|(US12422425 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20260016458 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|Title\|(US11644454 B2)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US20220404329 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(WO2022271842 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(AU2022299180 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(AU2022299180 A9)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(CA3207124 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US20230273174 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US11921098 B2)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4256520 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4256520 A4)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4256520 B1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4256520 C0)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4276752 A2)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4276752 A3)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(BR112023023226 A0)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(BR112023023226 A2)\|Verification methods and agronomic improvements for carbon removal based on improved rock weathering\|(BR112023023226 B1)\|Method to verify enhanced rock weathering using a mineral correction\|(US20240264139 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US12422425 B2)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(HK40094979 A)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(HK40095252 A)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US20260016458 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|Advantages / Prev. Drawbacks\|(US20220404329 A1)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(CA3207124 A1)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(US20230273174 A1)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(US11921098 B2)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(EP4276752 A2)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(US20240264139 A1)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|Independent Claims\|(US11644454 B2)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring (...) \|(US20220404329 A1)\| (...) A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring (...) \| (...) A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(WO2022271842 A1)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring (...) \|12. A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(CA3207124 A1)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring (...) \|12. A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(US20230273174 A1)\| (...) A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(US11921098 B2)\|1. A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(EP4256520 B1)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: (...) determining the fractional carbon dioxide removal by comparing the applied divalent cations to the measured divalent cations in the soil sample.\|(EP4276752 A2)\|1. A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(US20240264139 A1)\| (...) A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral comprising a comminuted silicate mineral and a binder, the comminuted silicate mineral having an average particle size between about 80 μm and about 100 μm; and immobile trace elements, the immobile (...) \|(US12422425 B2)\|1. A mineral amendment for enhanced rock weathering comprising: (...) \|(US20260016458 A1)\| (...) A method for verifying enhanced rock weathering using a mineral amendment comprising: (...) \|	Analysis of biological materials\|Basic materials chemistry\|Computer technology\|Electrical machinery, apparatus, energy\|Environmental technology\|Telecommunications	B01D-053/62\|B01D-2253/106\|B01D-2253/304\|B01D-2257/504\|C09K-011/77\|C09K-017/00\|C09K-017/12\|G01N-033/24\|H01J-049/10/5\|Y02C-020/40		B01D-053/62\|B01D-2253/106\|B01D-2253/304\|B01D-2257/504\|C09K-011/77\|C09K-017/00\|C09K-017/12\|G01N-033/24\|H01J-049/10/5\|Y02C-020/40	B01D-053/34\|B01D-053/62\|C09K-011/77\|C09K-017/00\|C09K-017/12\|G01N-033/24\|G06T-007/00\|G06T-007/60\|G16C-020/20\|G16C-020/70\|H01J-049/10	B01D-053/34\|B01D-053/62\|C09K-011/77\|C09K-017/00\|C09K-017/12\|G01N-033/24\|G06T-007/00\|G06T-007/60\|G16C-020/20\|G16C-020/70\|H01J-049/10			WO2024156029\|US20240383758\|US12422425	WO2024156029 110849874 WHO=Examiner SELF=N CAT=X\|US20240383758 112187058 WHO=Examiner SELF=N CAT=103\|US12422425 103013820 WHO=Examiner SELF=Y	US20210144935\|US20210144935\|US20210144935\|JP07088362\|US11921098\|US20220065103\|US20210144935\|US20190086381\|US20180082794\|US6753957\|US3864140\|US3853573\|US3856545	US20210144935 94130659 WHO=Examiner SELF=N CAT=A\|US20210144935 94130659 WHO=Examiner SELF=N CAT=A\|US20210144935 94130659 WHO=Examiner SELF=N CAT=A\|JP07088362 24293047 WHO=Examiner SELF=N CAT=A\|US11921098 103013820 WHO=Examiner SELF=Y\|US20220065103 98850983 WHO=Examiner SELF=N\|US20210144935 94130659 WHO=Applicant SELF=N\|US20190086381 83774390 WHO=Examiner SELF=N\|US20180082794 79099270 WHO=Examiner SELF=N\|US6753957 43373580 WHO=Examiner SELF=N\|US3864140 42244845 WHO=Examiner SELF=N\|US3853573 42252986 WHO=Examiner SELF=N\|US3856545 42260687 WHO=Examiner SELF=N		\|US11921098\|\|US3853573; US3856545; US3864140\|XP093021187; XP093021188; XP086574323; XP093021190; US20210144935\|\|\|US20210144935; XP086574323; XP093052931; XP093207104; XP085383712\|US20210144935; XP086574323; JP07088362; XP055822446\|\|\|US6753957; US20180082794; US20190086381; US20220065103; US20210144935	(EP4256520)\|Search Report references [Examiner]\|-PAULO CARLOS ET AL: "Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 129, 6 April 2021 (2021-04-06), XP086574323, ISSN: 0883-2927, [retrieved on 20210406], DOI: 10.1016/J.APGEOCHEM.2021.104955\|-MOOSDORF NILS ET AL: "Carbon Dioxide Efficiency of Terrestrial Enhanced Weathering", ENVIRONMENTAL SCIENCE & TECHNOLOGY, vol. 48, no. 9, 8 April 2014 (2014-04-08), US, pages 4809 - 4816, XP093052931, ISSN: 0013-936X, DOI: 10.1021/es4052022\|-LIU PU-LING ET AL: "Stable rare earth element tracers to evaluate soil erosion", SOIL AND TILLAGE RESEARCH, vol. 76, no. 2, 1 April 2004 (2004-04-01), NL, pages 147 - 155, XP093207104, ISSN: 0167-1987, DOI: 10.1016/j.still.2003.09.005\|-See also references of WO 2022271842A1\|-POTORT� ANGELA GIORGIA ET AL: "Traceability of Protected Geographical Indication (PGI) Interdonato lemon pulps by chemometric analysis of the mineral composition", JOURNAL OF FOOD COMPOSITION AND ANALYSIS, ELSEVIER, AMSTERDAM, NL, vol. 69, 15 March 2018 (2018-03-15), pages 122 - 128, XP085383712, ISSN: 0889-1575, DOI: 10.1016/J.JFCA.2018.03.001\|-C. Paulo et al, Applied Geochemistry, 2021, 219, 104955\|-N. Moosdorf et al, Environ. Sci. Tech., 2014, 48, 4809\|\|(EP4276752)\|Applicant references\|-PAULO CARLOS ET AL: "Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 129, 6 April 2021 (2021-04-06), XP086574323, ISSN: 0883-2927, [retrieved on 20210406], DOI: 10.1016/J.APGEOCHEM.2021.104955\|-SANNA A. ET AL: "A review of mineral carbonation technologies to sequester CO 2", CHEMICAL SOCIETY REVIEWS, vol. 43, no. 23, 1 January 2014 (2014-01-01), UK, pages 8049 - 8080, XP055822446, ISSN: 0306-0012, DOI: 10.1039/C4CS00035H\|\|(US12422425)\|Examiner references\|\|\|(US11644454)\|Applicant references\|-Haque et al. “Alkaline Mineral Soil Amendment: A Climate Change ‘Stabilization Wedge’?” Energies. 2019; 12 (12):2299. https://doi.org/10.3390/en12122299, Abstract; p. 8, para 2, 3.\|-Haque et al. “Risk assessment of Nl, Cr, and Si release from alkaline minerals during enhanced weathering” Open Agriculture, vol. 5, No. 1, 2020, doi: https://doi.org/10.1515/opag-2020-0016, Abstract; p. 167 para 4-p. 168 para 1; p. 169, para 2.\|-Paulo et al. “Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization.” Applied Geochemistry. Apr. 6, 2021, 129. 104955. 10.1016/j.apgeochem.2021. 104955. entire document.\|-Strefler et al. (2018). “Potential and costs of carbon dioxide removal by enhanced weathering of rocks.” Environmental Research Letters. 13. 10.1088/1748-9326/aaa9c4. entire document.\|-International Search Report and Written Opinion of the International Searching Authority for International Patent App. No. PCT/US22/34546 dated Nov. 15, 2022. (10 pages).\|\|\|(WO2022/271842)\|International Search Report [Examiner]\|-HAQUE FATIMA, CHIANG YI, SANTOS RAFAEL: "Alkaline Mineral Soil Amendment: A Climate Change ‘Stabilization Wedge’?", ENERGIES, vol. 12, no. 12, pages 2299, XP093021187, DOI: 10.3390/en12122299\|-HAQUE FATIMA, CHIANG YI WAI, SANTOS RAFAEL M.: "Risk assessment of Ni, Cr, and Si release from alkaline minerals during enhanced weathering", OPEN AGRICULTURE, vol. 5, no. 1, 1 January 2020 (2020-01-01), pages 166 - 175, XP093021188, DOI: 10.1515/opag-2020-0016\|-PAULO CARLOS; POWER IAN M.; STUBBS AMANDA R.; WANG BAOLIN; ZEYEN NINA; WILSON SIOBHAN A.: "Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 129, 6 April 2021 (2021-04-06), AMSTERDAM, NL , XP086574323, ISSN: 0883-2927, DOI: 10.1016/j.apgeochem.2021.104955\|-GREGORY UPSCALING, NEMET F, CALLAGHAN MAX W, FELIX, STREFLER JESSICA, AMANN THORBEN, BAUER NICO, KRIEGLER ELMAR, HARTMANN JENS: " Potential and costs of carbon dioxide removal by enhanced weathering of rocks", ENVIRONMENTAL RESEARCH LETTERS, 1 January 2018 (2018-01-01), pages 34010, XP093021190, Retrieved from the Internet <URL:https://iopscience.iop.org/article/10.1088/1748-9326/aaa9c4/pdf> [retrieved on 20230206]\|-See also references of EP 4256520A4\|\|\|\|\|\|	GRANTED	(EP4256520)\|GRANTED\|(EP4276752)\|PENDING\|(US12422425)\|GRANTED\|(US11921098)\|GRANTED\|(US11644454)\|GRANTED\|(US20260016458)\|PENDING\|(WO2022/271842)\|LAPSED\|(BR112023023226)\|GRANTED\|(AU2022299180)\|PENDING\|(HK40095252)\|PENDING\|(HK40094979)\|PENDING\|(CA3207124)\|PENDING	ALIVE	(EP4256520)\|ALIVE\|(EP4276752)\|ALIVE\|(US12422425)\|ALIVE\|(US11921098)\|ALIVE\|(US11644454)\|ALIVE\|(US20260016458)\|ALIVE\|(WO2022/271842)\|DEAD\|(BR112023023226)\|ALIVE\|(AU2022299180)\|ALIVE\|(HK40095252)\|ALIVE\|(HK40094979)\|ALIVE\|(CA3207124)\|ALIVE	(EP4256520)\|LEGAL DETAILS FOR EP4256520\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2022-06-22\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP22829238\|Application date=2022-06-22\|Standardized application number=2022EP-0829238\|Event publication date=2022-12-30\|Event code=EP/STAAPCT\|Event group=Examination events Entry into national phase\|The international publication has been made\|Original code: STAA\|Event publication date=2023-09-08\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2023-09-08\|Event code=EP/STAARQ\|Event indicator=Pos\|Event group=Examination events\|Request for examination was made\|Original code: STAA\|Event publication date=2023-10-11\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP4256520\|Publication stage code=A1\|Publication date=2023-10-11\|Standardized publication number=EP4256520\|Event publication date=2023-10-11\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2023-07-03\|Event publication date=2023-10-11\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2024-09-25\|Event code=EP/DAV\|Event indicator=Neg\|Event group=Designated states\|Request for validation of the European patent (deleted)\|Request for validation of the european patent (in any country) deleted\|Event publication 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code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2023-10-13\|Event code=EP/STAAPB\|Event group=Examination events\|The application has been published\|Original code: STAA\|Event publication date=2023-11-15\|Event code=EP/A2\|Event group=Examination events\|Application published without search report\|Publication country=EP\|Publication number=EP4276752\|Publication stage code=A2\|Publication date=2023-11-15\|Standardized publication number=EP4276752\|Event publication date=2023-11-15\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication 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modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2024-07-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2024-07-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2024-07-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2025-01-03\|Event code=EP/STAARQ\|Event indicator=Pos\|Event group=Examination events\|Request for examination was made\|Original code: STAA\|Event publication date=2025-02-05\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2024-12-31\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected 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group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2024-02-07\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2024-04-12\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2024-04-15\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2024-04-15\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2024-04-16\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2024-08-08\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20240264139\|Publication stage code=A1\|Publication date=2024-08-08\|Standardized publication number=US20240264139\|Event publication date=2024-08-08\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2024-08-10\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2024-09-07\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2024-09-09\|Event code=US/DBLNF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection - Double Patenting\|RJD=2024-09-09\|R4R=DBL\|RJST=non-final\|Rejected claims 1-10\|RJCT=2009US-11921098\|Event publication date=2024-09-17\|Event code=US/M327\|Event group=Examination events OAO\|Miscellaneous Communication to Applicant - No Action Count\|Event publication date=2024-12-10\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2025-02-12\|Event code=US/CTFR\|Event group=Examination events OA OAO\|Final Rejection\|Event publication date=2025-02-18\|Event code=US/DBLFR\|Event indicator=Neg\|Event group=Examination events\|Final rejection - Double Patenting\|RJD=2025-02-18\|R4R=DBL\|RJST=final\|Rejected claims 1-10\|RJCT=2009US-11921098\|Event publication date=2025-04-11\|Event code=US/INVSUM\|Event group=Examination events OAI INT\|Interview Summary- Applicant Initiated\|Event publication date=2025-04-13\|Event code=US/EXIN\|Event group=Examination events OAO INT\|Examiner Interview Summary Record (PTOL - 413)\|Event publication date=2025-05-27\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2025-05-28\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2025-08-27\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2025-08-27\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2025-08-27\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:WOLF, ADAM;CHANG, ELLIOT SUK-HYUN;TANK, ALAN ROBERT\|Reel/frame:072562/0621\|OWNER:EION CORP., NEW JERSEY\|Effective date of the event=2022-07-22\|Event publication date=2025-08-28\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2025-09-10\|Event code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=2025-09-10\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2025-09-23\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US12422425\|Publication stage code=B2\|Publication date=2025-09-23\|Standardized publication number=US12422425\|Event publication date=2025-09-23\|Event code=US/MEPGNTF\|Event group=Event indicating In Force Administrative notifications\|Mail Patent eGrant Notification\|Event publication date=2025-09-23\|Event code=US/EPGNTF\|Event group=Event indicating In Force Administrative notifications\|Patent eGrant Notification\|Event publication date=2025-09-23\|Event code=US/EPG\|Event group=Event indicating In Force\|Recordation of Patent eGrant\|Event publication date=2025-09-23\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=0\|(US11921098)\|LEGAL DETAILS FOR US11921098\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2023-03-30\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US18128583\|Application date=2023-03-30\|Standardized application number=2023US-18128583\|Event publication date=2023-03-30\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:NGUYEN, KIET TUAN\|Event publication date=2023-03-30\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=2881\|Event publication date=2023-03-30\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 27593-0773011\|Event publication date=2023-03-30\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 26874\|Event publication date=2023-03-30\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2023-03-30\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2023-03-30\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:WOLF, ADAM;CHANG, ELLIOT SUK-HYUN;TANK, ALAN ROBERT\|Reel/frame:063178/0691\|OWNER:EION CORP., NEW JERSEY\|Effective date of the event=2022-07-22\|Event publication date=2023-03-30\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2023-05-03\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2023-05-22\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2023-05-23\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-05-23\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2023-08-31\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20230273174\|Publication stage code=A1\|Publication date=2023-08-31\|Standardized publication number=US20230273174\|Event publication date=2023-08-31\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2023-10-01\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-10-27\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication 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publication date=2024-03-05\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US11921098\|Publication stage code=B2\|Publication date=2024-03-05\|Standardized publication number=US11921098\|Event publication date=2024-03-05\|Event code=US/MEPGNTF\|Event group=Event indicating In Force Administrative notifications\|Mail Patent eGrant Notification\|Event publication date=2024-03-05\|Event code=US/EPGNTF\|Event group=Event indicating In Force Administrative notifications\|Patent eGrant Notification\|Event publication date=2024-03-05\|Event code=US/EPG\|Event group=Event indicating In Force\|Recordation of Patent eGrant\|Event publication date=2024-03-05\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=0\|(US11644454)\|LEGAL DETAILS FOR US11644454\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2022-06-22\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US17846838\|Application date=2022-06-22\|Standardized application number=2022US-17846838\|Event publication date=2022-06-22\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:NGUYEN, KIET TUAN\|Event publication date=2022-06-22\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=2881\|Event publication date=2022-06-22\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 45665-0006\|Event publication date=2022-06-22\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 69082\|Event publication date=2022-06-22\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2022-06-22\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2022-06-22\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2022-06-22\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2022-07-07\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2022-07-08\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2022-08-03\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2022-09-02\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:WOLF, ADAM;CHANG, ELLIOT SUK-HYUN;TANK, ALAN ROBERT\|Reel/frame:060976/0081\|OWNER:EION CORP., NEW JERSEY\|Effective date of the event=2022-07-22\|Event publication date=2022-10-06\|Event code=US/POAC\|Event group=Change of name or address\|Change in Power of Attorney (May Include Associate POA)\|Event publication date=2022-12-16\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2022-12-16\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2022-12-16\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2022-12-22\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20220404329\|Publication stage code=A1\|Publication date=2022-12-22\|Standardized publication number=US20220404329\|Event publication date=2022-12-22\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2023-02-02\|Event code=US/PDPH\|Event group=ACL Examination events\|Petition Decision PPH Decision\|Event publication date=2023-02-06\|Event code=US/PETDGMS\|Event group=ACL\|Record Petition Decision of Granted to Make Special\|Event publication date=2023-02-12\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-03-02\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2023-03-06\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2023-03-10\|Event code=US/ODPD8\|Event group=AMD\|Letter Withdrawing a Notice Requiring Inventor Oath or Declaration\|Event publication date=2023-03-13\|Event code=US/MODPD8\|Event group=Administrative notifications\|Mail Letter Withdrawing a Notice Requiring Inventor Oath or Declaration\|Event publication date=2023-03-29\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2023-03-29\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2023-04-03\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2023-04-19\|Event code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=2023-04-19\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2023-05-09\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US11644454\|Publication stage code=B2\|Publication date=2023-05-09\|Standardized publication number=US11644454\|Event publication date=2023-05-09\|Event code=US/MEPGNTF\|Event group=Event indicating In Force Administrative notifications\|Mail Patent eGrant Notification\|Event publication date=2023-05-09\|Event code=US/EPGNTF\|Event group=Event indicating In Force Administrative notifications\|Patent eGrant Notification\|Event publication date=2023-05-09\|Event code=US/EPG\|Event group=Event indicating In Force\|Recordation of Patent eGrant\|Event publication date=2023-05-09\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=0\|(US20260016458)\|LEGAL DETAILS FOR US20260016458\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-09-22\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19335929\|Application date=2025-09-22\|Standardized application number=2025US-19335929\|Event publication date=2025-09-22\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-09-22\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-09-22\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 0153961-0810853\|Event publication date=2025-09-22\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 26874\|Event publication date=2025-09-22\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2025-09-22\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-09-22\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-09-22\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-10-08\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2025-10-09\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-10-09\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-10-09\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-11-18\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2026-01-15\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20260016458\|Publication stage code=A1\|Publication date=2026-01-15\|Standardized publication number=US20260016458\|Event publication date=2026-01-16\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|(WO2022/271842)\|LEGAL DETAILS FOR WO2022/271842\|Actual or expected expiration date=2024-12-22\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-06-22\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2022/034546\|Application date=2022-06-22\|Standardized application number=2022WO-US34546\|Event publication date=2022-12-29\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2022/271842\|Publication stage code=A1\|Publication date=2022-12-29\|Standardized publication number=WO2022271842\|Event publication date=2024-12-22\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2022299180\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2022299180\|Application date in the designated or member state=2022-06-22\|Application number in the designated or member state=2022AU-0299180\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2022299180\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2023-07-13\|Publication number in the designated or member state=AU2022299180\|Event publication date=2023-07-13\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=AU\|MEMBER STATE LEGAL DETAILS FOR BR112023023226\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=BR Corresponding appl: BR112023023226\|Application date in the designated or member state=2022-06-22\|Application number in the designated or member state=2023BR-0023226\|Corresponding cc:\|Designated or member state=BR Corresponding pat: BR112023023226\|Publication stage code in the designated or member state=A0\|Publication date in the designated or member state=2023-11-14\|Publication number in the designated or member state=BR112023023226\|Event publication date=2023-11-14\|Event code=WO/REG\|Event code=BR/B01A\|Event group=Examination events\|Reference to a national code\|Pct publication - request for entry into the national phase\|Comunicacao da publicacao internacional pct. apresentacao de peticao de requerimento de entrada na fase nacional\|Corresponding cc:\|Designated or member state=BR\|Event publication date=2024-01-30\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2023-11-06\|Corresponding cc:\|Designated or member state=BR\|MEMBER STATE LEGAL DETAILS FOR CA3207124\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA3207124\|Application date in the designated or member state=2022-06-22\|Application number in the designated or member state=2022CA-3207124\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA3207124\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2022-12-29\|Publication number in the designated or member state=CA3207124\|Event publication date=2023-06-29\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2024-01-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2024-01-23\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP4256520\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP22829238\|Application date in the designated or member state=2022-06-22\|Application number in the designated or member state=2022EP-0829238\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP4256520\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2023-10-11\|Publication number in the designated or member state=EP4256520\|Event publication date=2023-02-08\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2023-07-16\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2023-07-03\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2025-12-10\|Event code=WO/WWG\|Event indicator=Pos\|Event group=Event indicating In Force\|Wipo information: grant in national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR HK40095252\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=HK Corresponding appl: HK62023083672\|Application date in the designated or member state=2023-12-05\|Application number in the designated or member state=2023HK-6083672\|Corresponding cc:\|Designated or member state=HK Corresponding pat: HK40095252\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2024-01-26\|Publication number in the designated or member state=HK40095252\|(BR112023023226)\|LEGAL DETAILS FOR BR112023023226\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2022-06-22\|Event code=BR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=BR BR112023023226\|Application date=2022-06-22\|Standardized application number=2023BR-0023226\|Event publication date=2023-11-14\|Event code=BR/A0\|Event indicator=Pos\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=BR\|Publication number=BR112023023226\|Publication stage code=A0\|Publication date=2023-11-14\|Standardized publication number=BR112023023226\|Event publication date=2024-01-30\|Event code=BR/A2\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention / pipeline patent published without search report\|Publication country=BR\|Publication number=BR112023023226\|Publication stage code=A2\|Publication date=2024-01-30\|Standardized publication number=BR112023023226\|Event publication date=2025-09-30\|Event code=BR/B07A\|Event group=Examination events\|Technical examination (opinion): publication of technical examination (opinion)\|Ciencia de parecer: conhecimento de parecer tecnico [codigo 7.1 rpi]\|Event publication date=2025-12-16\|Event code=BR/B09A\|Event group=Event indicating In Force Administrative notifications\|Decision: granting\|Decisao: deferimento [codigo 9.1 rpi]\|Event publication date=2026-01-13\|Event code=BR/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent / Granted pipeline patent\|Publication country=BR\|Publication number=BR112023023226\|Publication stage code=B1\|Publication date=2026-01-13\|Standardized publication number=BR112023023226\|Event publication date=2026-01-13\|Event code=BR/B16A\|Event indicator=Pos\|Event group=Event indicating In Force Administrative notifications\|Patent or certificate of addition of invention granted\|Concessao de patente ou certificado de adicao de invencao [codigo 16.1 rpi]\|Prazo de validade: 20 (VINTE) ANOS CONTADOS A PARTIR DE 22/06/2022, OBSERVADAS AS CONDICOES LEGAIS\|(AU2022299180)\|LEGAL DETAILS FOR AU2022299180\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-06-22\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2022299180\|Application date=2022-06-22\|Standardized application number=2022AU-0299180\|Event publication date=2023-07-13\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2022299180\|Publication stage code=A1\|Publication date=2023-07-13\|Standardized publication number=AU2022299180\|Event publication date=2024-10-24\|Event code=AU/A9\|Event indicator=Pos\|Event group=Examination events\|Corrected complete document\|Publication country=AU\|Publication number=AU2022299180\|Publication stage code=A9\|Publication date=2024-10-24\|Standardized publication number=AU2022299180\|Event publication date=2024-10-24\|Event code=AU/SREP\|Event group=Administrative notifications\|Specification republished\|(HK40095252)\|LEGAL DETAILS FOR HK40095252\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-12-05\|Event code=HK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=HK HK62023083672\|Application date=2023-12-05\|Standardized application number=2023HK-6083672\|Event publication date=2024-01-26\|Event code=HK/A\|Event indicator=Pos\|Event group=Examination events\|Standard patent (R) application\|Publication country=HK\|Publication number=HK40095252\|Publication stage code=A\|Publication date=2024-01-26\|Standardized publication number=HK40095252\|(HK40094979)\|LEGAL DETAILS FOR HK40094979\|Actual or expected expiration date=2043-12-05\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-12-05\|Event code=HK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=HK HK42023083673\|Application date=2023-12-05\|Standardized application number=2023HK-4083673\|Event publication date=2024-01-26\|Event code=HK/A\|Event indicator=Pos\|Event group=Examination events\|Standard patent (R) application\|Publication country=HK\|Publication number=HK40094979\|Publication stage code=A\|Publication date=2024-01-26\|Standardized publication number=HK40094979\|(CA3207124)\|LEGAL DETAILS FOR CA3207124\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-06-22\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA3207124\|Application date=2022-06-22\|Standardized application number=2022CA-3207124\|Event publication date=2022-12-29\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA3207124\|Publication stage code=A1\|Publication date=2022-12-29\|Standardized publication number=CA3207124\|Event publication date=2025-06-13\|Event code=CA/MFA\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|MAINTENANCE FEE FOR APPLICATION PAID\|Annual fees payment date=2025-06-13\|Year of payment of annual fees=3\|Fee description text: MF (APPLICATION, 3RD ANNIV.) - STANDARD\|Event publication date=2025-06-13\|Event code=CA/U00\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FEE PAID\|ST27 STATUS EVENT CODE: A-1-1-U10-U00-U101 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE REQUEST RECEIVED\|Effective date of the event=2025-06-13\|Event publication date=2025-06-13\|Event code=CA/U11\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FULL RENEWAL OR MAINTENANCE FEE PAID\|ST27 STATUS EVENT CODE: A-1-1-U10-U11-U102 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE FEE PAYMENT PAID IN FULL\|Effective date of the event=2025-06-13\|Event publication date=2026-01-13\|Event code=CA/P22\|Event group=Classification modifications Corrections\|CLASSIFICATION MODIFIED\|ST27 STATUS EVENT CODE: A-1-1-P10-P22-P110 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: CLASSIFICATION MODIFIED\|Effective date of the event=2026-01-13	(EP4256520)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4256520)\|UP Participating States: EE, DE, BE, FI, PT, BG, DK, MT, LT, LU, LV, IT, FR, SE, AT, SI, RO, NL\|(EP4276752)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4276752)\|Extension States: ME, BA\|(EP4276752)\|Validation States: MA, MD, TN, KH\|(WO2022/271842)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2022/271842)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2022/271842)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2022/271842)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2022/271842)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP4256520)\|EP; AT; BE; BG; CH; DE; DK; EE; EP; FI; FR; GB; HK; IE; IT; LT; LU; LV; MT; NL; PT; RO; SE; SI\|(EP4276752)\|EP; EP; HK\|(US12422425)\|US\|(US11921098)\|US\|(US11644454)\|US\|(US20260016458)\|US\|(WO2022/271842)\|AU; BR; CA; EP; 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Spruce St., Princeton, New Jersey 08542 , COUNTRY=US\|(US11921098)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US , ATYP=US Company\|(US20230273174)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US\|(WO2022/271842)\|NAME=EION CORP. 82 Spruce St. Princeton, New Jersey 08542 , COUNTRY=US\|(US11644454)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US , ATYP=US Company\|(US20220404329)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US	(EP4256520)\|IT\|(EP4256520)\|IT\|(EP4276752)\|IT\|(EP4276752)\|IT\|\|\|\|(WO2022/271842)\|US\|(AU2022299180)\|NZ\|(AU2022299180)\|NZ\|(HK40095252)\|HK\|(HK40094979)\|HK\|(CA3207124)\|CA	(EP4256520)\|NAME=Dragotti & Associati S.P.A. Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101869514\|(EP4256520)\|NAME=Pistolesi, Roberto;Dragotti & Associati Srl Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101195246\|(EP4276752)\|NAME=Dragotti & Associati S.R.L. Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101869514\|(EP4276752)\|NAME=Pistolesi, Roberto;Dragotti & Associati Srl Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101195246\|(US12422425)\|NAME=Frost Brown Todd LLP NAME=VanDrake, III Vance V. NAME=Johnson Alexander J.\|(US11921098)\|NAME=Frost Brown Todd LLP NAME=VanDrake, III Vance V. NAME=Johnson Alexander J.\|(US11644454)\|NAME=Ulmer & Berne LLP NAME=Van Drake, III Vance V. NAME=Johnson Alexander J.\|(WO2022/271842)\|NAME=FALK, Daniel T. et al. 1660 W. 2nd Street Suite 1100 Cleveland, Ohio 44113 , POSTCODE=44113 , COUNTRY=US\|(AU2022299180)\|NAME=AJ Pietras IP Limited Level 2, Bloomfield House 46/50 Bloomfield Terrace , CITY=Lower Hutt , STATE=Wellington , POSTCODE=5010 , COUNTRY=NZ\|(AU2022299180)\|NAME=AJ Pietras IP Limited Level 1, 29 Kings Crescent , CITY=Lower Hutt , STATE=Wellington , POSTCODE=5010 , COUNTRY=NZ\|(HK40095252)\|NAME=HNC INNOVATION LIMITED , COUNTRY=HK\|(HK40094979)\|NAME=HNC INNOVATION LIMITED , COUNTRY=HK\|(CA3207124)\|NAME=BURNET, DUCKWORTH & PALMER LLP , COUNTRY=CA	\|(EP4256520)\|US; US; US\|\|(EP4256520)\|US; US; US\|(EP4276752)\|US; US; US\|(EP4276752)\|US; US; US\|(US12422425)\|US; US; US\|(US20240264139)\|US; US; US\|(US11921098)\|US; US; US\|(US20230273174)\|US; US; US\|(US11644454)\|US; US; US\|(US20220404329)\|US; US; US\|(US20260016458)\|US; US; US\|(WO2022/271842)\|US; US; US\|\|\|\|\|\|\|(CA3207124)\|US; US; US	(EP4256520)\|NAME=WOLF, Adam\|NAME=CHANG, Elliot Suk-Hyun\|NAME=TANK, Alan Robert\|(EP4256520)\|NAME=WOLF, Adam, CITY=Princeton, New Jersey 08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun, CITY=Berkeley, California 94703, COUNTRY=US \|NAME=TANK, Alan Robert, CITY=Bethesda, Maryland 20816, COUNTRY=US\|(EP4256520)\|NAME=WOLF, Adam\|NAME=CHANG, Elliot Suk-Hyun\|NAME=TANK, Alan Robert\|(EP4256520)\|NAME=WOLF, Adam, CITY=Princeton, New Jersey 08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun, CITY=Berkeley, California 94703, COUNTRY=US \|NAME=TANK, Alan Robert, CITY=Bethesda, Maryland 20816, COUNTRY=US\|(EP4276752)\|NAME=WOLF, Adam, CITY=Princeton, 08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun, CITY=Foster City, 94404, COUNTRY=US \|NAME=TANK, Alan Robert, CITY=Bethesda, 20816, COUNTRY=US\|(EP4276752)\|NAME=WOLF, Adam, CITY=Princeton, 08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun, CITY=Foster City, 94404, COUNTRY=US \|NAME=TANK, Alan Robert, CITY=Bethesda, 20816, COUNTRY=US\|(US12422425)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US20240264139)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US11921098)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US20230273174)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US11644454)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US20220404329)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US20260016458)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(WO2022/271842)\|NAME=WOLF, Adam 82 Spruce St. Princeton, New Jersey 08542, POSTCODE=08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun 1905 Grant Street Berkeley, California 94703, POSTCODE=94703, COUNTRY=US \|NAME=TANK, Alan Robert 5324 Portsmouth Road Bethesda, Maryland 20816, POSTCODE=20816, COUNTRY=US\|(BR112023023226)\|NAME=WOLF ADAM\|NAME=CHANG ELLIOT SUK-HYUN\|NAME=TANK ALAN ROBERT\|(BR112023023226)\|NAME=WOLF ADAM\|NAME=CHANG ELLIOT SUK-HYUN\|NAME=TANK ALAN ROBERT\|(AU2022299180)\|NAME=WOLF, Adam\|NAME=CHANG, Elliot Suk-Hyun\|NAME=TANK, Alan Robert\|(AU2022299180)\|NAME=WOLF, Adam\|NAME=CHANG, Elliot Suk-Hyun\|NAME=TANK, Alan Robert\|(HK40095252)\|NAME=WOLF Adam\|NAME=CHANG Elliot Suk-Hyun\|NAME=TANK Alan Robert\|(HK40094979)\|NAME=WOLF Adam\|NAME=CHANG Elliot Suk-Hyun\|NAME=TANK Alan Robert\|(CA3207124)\|NAME=WOLF, ADAM, COUNTRY=US \|NAME=CHANG, ELLIOT SUK-HYUN, COUNTRY=US \|NAME=TANK, ALAN ROBERT, COUNTRY=US	(US20260016458)\|4\|(US12422425)\|4\|(US11921098)\|4\|(WO2022/271842)\|4\|\|(CA3207124)\|4\|(US11644454)\|4	9	12			(EP4256520)\|WO2022/271842\|(EP4276752)\|WO2022/271842\|(BR112023023226)\|WO2022/271842\|(AU2022299180)\|WO2022/271842\|(HK40095252)\|WO2022/271842\|(CA3207124)\|WO2022/271842	(EP4276752)\|EP22829238	(EP4256520)\|Gazette date: GAZDATE=2025-12-10\|\|(EP4256520)\|Number of Claims: NCL=8\|\|Primary examiner: Poole, Robert\|\|(EP4276752)\|Number of Claims: NCL=10\|22.09.2023 as a divisional application to the application mentioned under INID code 62.\|Primary examiner: Poole, Robert\|\|(US12422425)\|Number of Claims: NCL=10\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=0\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US20240264139)\|Number of Claims: NCL=10\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US11921098)\|Number of Claims: NCL=10\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US20230273174)\|Number of Claims: NCL=10\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US11644454)\|Number of Claims: NCL=11\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US20220404329)\|Number of Claims: NCL=21\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1,12\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US20260016458)\|Number of Claims: NCL=11\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|\|(WO2022/271842)\|Number of Claims: NCL=21\|Extended kind: EXTK=x\|\|(BR112023023226)\|Prazo de Validade: 20 (vinte) anos contados a partir de 22/06/2022, observadas as condições legais\|\|(CA3207124)\|Number of Claims: NCL=21\|	(EP4276752)\|Division of: EP22829238 FDD=2022-06-22 [2022EP-0829238]\|(US12422425)\|Continuation of: US18/128,583 FDD=2023-03-30 [2023US-18128583]\|Division of: US17/846,838 FDD=2022-06-22 [2022US-17846838]\|Continuation of: US11921098 \|Division of: US11644454 2023-04-19 [US11644454]\|Provisional Appl: US63/322,672 FDD=2022-03-23 [2022US-63322672]\|Provisional Appl: US63/289,395 FDD=2021-12-14 [2021US-63289395]\|Provisional Appl: US63/213,398 FDD=2021-06-22 [2021US-63213398]\|Previous publication: US20240264139 A1 2024-08-08 [US20240264139]\|(US11921098)\|Division of: US17/846,838 FDD=2022-06-22 [2022US-17846838]\|Division of: US11644454 \|Provisional Appl: US63/322,672 FDD=2022-03-23 [2022US-63322672]\|Provisional Appl: US63/289,395 FDD=2021-12-14 [2021US-63289395]\|Provisional Appl: US63/213,398 FDD=2021-06-22 [2021US-63213398]\|Previous publication: US20230273174 A1 2023-08-31 [US20230273174]\|(US11644454)\|Provisional Appl: US63/322,672 FDD=2022-03-23 [2022US-63322672]\|Provisional Appl: US63/289,395 FDD=2021-12-14 [2021US-63289395]\|Provisional Appl: US63/213,398 FDD=2021-06-22 [2021US-63213398]\|Previous publication: US20220404329 A1 2022-12-22 [US20220404329]\|(US20260016458)\|Continuation of: US18/435,492 FDD=2024-02-07 [2024US-18435492]\|Continuation of: US18/128,583 FDD=2023-03-30 [2023US-18128583]\|Division of: US17/846,838 FDD=2022-06-22 [2022US-17846838]\|Continuation of: US12422425 \|Continuation of: US11921098 \|Division of: US11644454 \|Provisional Appl: US63/213,398 FDD=2021-06-22 [2021US-63213398]\|Provisional Appl: US63/289,395 FDD=2021-12-14 [2021US-63289395]\|Provisional Appl: US63/322,672 FDD=2022-03-23 [2022US-63322672]\|(CA3207124)\|Division of: CA3207124 FDD=2022-06-22 [2022CA-3207124]	(EP4256520)\|ENGLISH (ENG)	(US20260016458)\|Patent\|(BR112023023226)\|Patent\|(EP4256520)\|Patent\|(EP4256520)\|Patent\|(US12422425)\|Patent\|(EP4256520)\|Patent\|(AU2022299180)\|Patent\|(US20240264139)\|Patent\|(EP4276752)\|Patent\|(US11921098)\|Patent\|(BR112023023226)\|Patent\|(HK40094979)\|Patent\|(HK40095252)\|Patent\|(EP4276752)\|Patent\|(BR112023023226)\|Patent\|(EP4256520)\|Patent\|(US20230273174)\|Patent\|(AU2022299180)\|Patent\|(US11644454)\|Patent\|(CA3207124)\|Patent\|(WO2022271842)\|Patent\|(US20220404329)\|Patent	Titre: (EP4256520)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering Résumé: (EP4256520)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.	3	Abstract	gpt-4o-mini	yes	The article discusses methods for verifying enhanced rock weathering and mentions mineral amendments that facilitate this process, which aligns with the goal of carbon sequestration through accelerated weathering.
3	US63/669,351P\|US19/264,502	US19/264,502	US20260017435	117356463	US20260017435 A1 2026-01-15 [US20260017435]	2024-07-10\|2025-07-09	2025-07-09	2026-01-15		(US20260017435)\|2045-07-09	(US20260017435)\|Technologies for modeling carbon dioxide removal	(US20260017435)\|Technologies for modeling carbon dioxide removal include a compute device with circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may also be configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Further, the circuitry may be configured to present a visual representation of the at least one prediction in a user interface. Other embodiments are also described and claimed.	UNIVERSITY INDIANA TRUSTEES	(US20260017435)\|THE TRUSTEES OF INDIANA UNIVERSITY ([US])	ZHU CHEN	(US20260017435)\|Zhu Chen		(US20260017435)\|A modeling forecast is useful at every stage of a project: conceptualization, contract negotiation, application, and post-project monitoring.\|There exists a plurality of advantages of the present disclosure arising from the various features of the apparatus, systems, and methods described herein.\|Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.\|	(US20260017435)\|1. A compute device comprising: circuitry configured to: obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and present a visual representation of the at least one prediction in a user interface.\|14. A method comprising: obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and presenting, by the compute device, a visual representation of the at least one prediction in a user interface.\|19. One or more machine-readable storage media comprising a plurality of instructions stored thereon that, in response to being executed, cause a compute device to: obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and present a visual representation of the at least one prediction in a user interface.\|	(US20260017435)\|Further, the system 100 provides provenance for the execution of tools, clonability, and reusability and integrates with national open cyberinfrastructure and public clouds for workflow execution.\|In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. The system 100, in operation, provides innovative and independent geochemical models and modeling forecasts, filling a current gap in monitoring, reporting, and verification (MRV).\|The present application discloses one or more of the features recited in the appended claims and/or the following features which, alone or in any combination, may comprise patentable subject matter:According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering.\|	(US20260017435)\|ENHANCED ROCK(100,28)\|MODELING CARBON DIOXIDE REMOVAL(100,6)\|IRON COPRECIPITATION(94,11)\|FORECAST MODEL(65,1)\|FORECASTING MODEL(65,1)\|VISUAL REPRESENTATION(59,20)\|WORKFLOW EXECUTION(57,1)\|NATIONAL OPEN CYBER INFRASTRUCTURE(56,1)\|SATISFYING CONCERN(54,1)\|PARAMETER DATA(53,57)\|OPEN CYBER INFRASTRUCTURE(47,1)\|GEOCHEMICAL MODEL(41,3)\|CONCEPTUALIZATION(36,1)\|CARBON DIOXIDE(33,77)\|CLONABILITY(32,1)\|REUSABILITY(32,1)\|NEGOTIATION(31,1)\|PROVENANCE(31,1)\|POST PROJECT MONITORING(30,1)\|ENHANCE REMOVAL(28,1)\|VERIFICATION(28,1)\|REPORTING(27,1)\|SCIENCE GATEWAY(27,1)\|COMPUTE DEVICE(26,45)\|BASALT WEATHERING(25,6)\|PUBLIC CLOUD(25,1)\|MODELING COMPUTE DEVICE(24,92)\|UNIDIRECTIONAL RATE(24,6)\|SOILS(23,1)\|GROUND(22,45)\|CARBON DIOXIDE REMOVAL(22,12)\|GATEWAY(21,15)\|TOXIC METAL(20,24)\|PREDICTION VISUAL REPRESENTATION(19,5)\|USER INTERFACE(16,21)\|LIBRARY(15,7)\|IRREVERSIBLE REACTION(15,6)\|MACHINE LEARNING MODEL(15,4)\|STORAGE MEDIA(14,3)\|HECTARE(13,12)\|BASALT TON(12,2)\|TOXIC METAL RELEASE(12,2)\|NEAR EQUILIBRIUM RATE(11,5)\|DATABASE(10,15)\|LOCATION DISTANCE(10,4)\|BLIND PORE(10,3)\|INTERACTIVE GRAPH(10,3)\|SOIL PARAMETER(10,3)\|NICKEL VISUAL REPRESENTATION(10,2)\|ACOUSTIC TOUCHSCREEN SENSOR(10,1)\|ENHANCED ROCK WEATHERING BATCH(10,1)\|SANDSTONE AQUIFER(10,1)\|SEMIEMPIRICAL SCALING FACTOR(10,1)\|WORLDWIDE INTEROPERABILITY(10,1)\|SUBSYSTEM(9,7)\|COMMUNICATION CIRCUITRY(9,6)\|OBTAINING PARAMETER DATA(9,6)\|PREDICTED(9,6)\|PROBABILITY(8,5)\|BASALT DENSITY(8,3)\|TOPSOIL LAYER(8,3)\|CYBER INFRASTRUCTURE(8,1)\|GEOCHEMICAL EXPERT(8,1)\|INFRARED TOUCHSCREEN SENSOR(8,1)\|LEVERAGE EXPERTIZE(8,1)\|MINE TAILING(8,1)\|RENDING ENGINE(8,1)\|WEB INTERFACE(7,5)\|BULK SOIL DENSITY(7,4)\|APPLICABLE REGULATION(7,2)\|NONVOLATILE MEMORY(7,2)\|SOIL DEPTH(7,2)\|BASALT MINERAL MAKEUP(7,1)\|GRAPHICAL PRESENTATION(7,1)\|INTERPRETABLE MODEL(7,1)\|MULTICHIP PACKAGE(7,1)\|NUMB INDICATIVE(7,1)\|PORTABLE NETWORK GRAPHICS(7,1)\|PURCHASER CORPORATION(7,1)\|RECONFIGURABLE HARDWARE(7,1)\|SIMILARITY SCORE(7,1)\|SIMILARITY DETERMINATION(6,3)\|STAKEHOLDER(6,3)\|AUTOMATIC DOCUMENTATION(6,1)\|BASALT MASS(6,1)\|BIODIVERSITY LOSS(6,1)\|CAPACITIVE TOUCHSCREEN SENSOR(6,1)\|CLUSTERING ANALYSIS(6,1)\|ENCODED INSTRUCTION(6,1)\|GROWING CONCERN(6,1)\|IRRIGATION WATER REGULATION(6,1)\|OXY HYDROXIDE(6,1)\|PARAMETER DATA REFORMATTING(6,1)\|RESISTIVE TOUCHSCREEN SENSOR(6,1)\|SIMULATION CONFIDENCE INTERVAL(6,1)\|SOIL REGULATION(6,1)\|SPECIALIZED HARDWARE(6,1)\|VISUAL PRESENTATION(6,1)\|CADMIUM(5,4)\|CHROMIUM(5,4)\|AIR CALCULATION(5,2)\|CUBIC CENTIMETER(5,2)\|DRINKING WATER REGULATION(5,2)\|GEOCHEMICAL MODELING(5,2)\|GEOGRAPHIC COORDINATE(5,2)\|NONEXPERT(5,2)\|PHREEQC(5,2)\|CARBON CAPTURE PREDICTION(5,1)\|CARBON CAPTURE SIMULATION(5,1)\|CARBON CREDIT MARKET(5,1)\|COAXIAL NETWORK(5,1)\|COMPLEX INTERACTION(5,1)\|CONTROLLER CHIP(5,1)\|CREDIT ABILITY(5,1)\|DIGITAL VERSION(5,1)\|ENHANCE CAPTURE(5,1)\|FEED STOCK(5,1)\|FILE FORMAT(5,1)\|FIRMWARE CODE(5,1)\|HARDWARE CIRCUITRY(5,1)\|MICROWAVE ACCESS(5,1)\|OPTICAL IMAGING TOUCHSCREEN SENSOR(5,1)\|PREDICATION(5,1)\|SIMULATION PRODUCT(5,1)\|WEB MODEL INTERFACE(5,1)\|GRAM(4,3)\|USER INPUT(4,3)\|PREDICTION ACCURACY(4,2)\|ADJUSTED PARAMETER(3,1)\|ARCHIVE(3,1)\|AUTHORIZATION(3,1)\|BLUETOOTH(3,1)\|BUS LINK(3,1)\|CARBON DIOXIDE TRAP ENERGY(3,1)\|CERTIFICATION(3,1)\|CHIPSET(3,1)\|COPRECIPITATION(3,1)\|COSINE SIMILARITY(3,1)\|DAUGHTER CARD(3,1)\|DISRUPTION(3,1)\|DROUGHT(3,1)\|ENCODING(3,1)\|ENSEMBLE(3,1)\|EXECUTABLE(3,1)\|FACILITY(3,1)\|FIBER NETWORK(3,1)\|FIND PATTERN(3,1)\|FLOODING(3,1)\|GEOLOGICAL SURVEY(3,1)\|GESTURE(3,1)\|GIGATON LEVEL(3,1)\|GREENHOUSE GAS ATMOSPHERE(3,1)\|HYPERTEXT MARKUP LANGUAGE(3,1)\|IDENTIFICATION(3,1)\|INCLUSION(3,1)\|INDUSTRY STANDARD AUTHENTICATION(3,1)\|INTEGRATED SENSOR HUB(3,1)\|KEYBOARD(3,1)\|LYSIMETER EXPERIMENTAL DATA(3,1)\|MAKE MODELING(3,1)\|	(US20260017435)\|1. A compute device comprising:\| circuitry configured to:\| obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering;\| produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| present a visual representation of the at least one prediction in a user interface.\|2. The compute device of claim 1, wherein to produce, using one or more models from a library of models, at least one prediction comprises to simulate basalt weathering as irreversible reactions with unidirectional rates.\|3. The compute device of claim 1, wherein to produce, using one or more models from a library of models, at least one prediction comprises to utilize one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates.\|4. The compute device of claim 1, wherein to produce, using one or more models from a library of models, at least one prediction comprises to utilize one or more models that simulate co-precipitation of iron with toxic metals.\|5. The compute device of claim 1, wherein to obtain parameter data comprises to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured.\|6. The compute device of claim 1, wherein to obtain parameter data comprises to obtain the parameter data as a function of an identification of the location where the carbon dioxide is to be captured.\|7. The compute device of claim 1, wherein the circuitry is further configured to calculate, as a function of the obtained parameter data, additional parameter data for use by the one or more models.\|8. The compute device of claim 1, wherein to produce at least one prediction comprises to select one or more models as a function of the obtained parameter data.\|9. The compute device of claim 1, wherein to produce at least one prediction comprises to select one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library.\|10. The compute device of claim 1, wherein to produce at least one prediction comprises to utilize one or more machine learning models.\|11. The compute device of claim 1, wherein to produce at least one prediction comprises to produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period.\|12. The compute device of claim 1, wherein to produce at least one prediction comprises to produce one or more predictions indicative of tons of carbon dioxide captured per unit of area.\|13. The compute device of claim 1, wherein to produce at least one prediction comprises to produce at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured.\|14. A method comprising:\| obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering;\| producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| presenting, by the compute device, a visual representation of the at least one prediction in a user interface.\|15. The method of claim 14, wherein producing, using one or more models from a library of models, at least one prediction comprises simulating basalt weathering as irreversible reactions with unidirectional rates.\|16. The method of claim 14, wherein producing, using one or more models from a library of models, at least one prediction comprises utilizing one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates.\|17. The method of claim 14, wherein producing, using one or more models from a library of models, at least one prediction comprises utilizing one or more models that simulate co-precipitation of iron with toxic metals.\|18. The method of claim 14, wherein obtaining parameter data comprises obtaining data indicative of properties of soil in a location where the carbon dioxide is to be captured.\|19. One or more machine-readable storage media comprising a plurality of instructions stored thereon that, in response to being executed, cause a compute device to:\| obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering;\| produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| present a visual representation of the at least one prediction in a user interface.\|20. The one or more machine-readable storage media of claim 19, wherein to obtain parameter data comprises to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured.	(US20260017435)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/669,351 filed on Jul. 10, 2024, the disclosure of which is expressly incorporated herein.\|(US20260017435)\|BACKGROUND\|[0002] Climate change is a growing concern across the world as atmospheric greenhouse gases such as carbon dioxide trap energy radiated from the sun. While a direct result of increases in greenhouse gases is increased temperatures on Earth, knock on effects include droughts, flooding, loss of biodiversity, and disruptions in energy and transportation systems across the world. Through interactions between water and rock (e.g., in soil), carbon dioxide can be captured (e.g., removed) from the atmosphere and correspondingly lessen the effects of climate change. However, given the multitude of factors that influence the complex interactions between water and rock, it is not feasible in conventional computerized systems to reliably determine the amount of carbon dioxide that will be removed in a given location, under a given set of conditions, or to predict side effects of any efforts to enhance the capture of carbon dioxide in the soil. Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.\|SUMMARY\|[0003] The present application discloses one or more of the features recited in the appended claims and/or the following features which, alone or in any combination, may comprise patentable subject matter:\|[0004] According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may be further configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. Producing a prediction may include simulating co-precipitation of iron with one or more toxic metals. The circuitry may be further configured to present a visual representation of the at least one prediction in a user interface.\|[0005] In some embodiments, the circuitry may be configured such that using one or more models from a library of models to produce at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. The circuitry may also be configured to utilize one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, the circuitry may be configured to utilize one or more models that simulate co-precipitation of iron with toxic metals. The circuitry may be configured to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that obtaining data indicative of properties of soil includes obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and basalt mineral composition.\|[0006] The circuitry may be configured such that obtaining parameter data includes obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured to obtain parameter data as a function of an identification of the location where the carbon dioxide is to be captured by reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. The circuitry may be configured to obtain parameter data through user input into corresponding fields of a user interface. In some embodiments, the circuitry may be further configured to calculate, as a function of the obtained parameter data, additional parameter data for use by the one or more models. The circuitry may be configured such that calculating additional parameter data involves calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.\|[0007] In some embodiments, calculating additional parameter data further includes utilizing a database of specific surface areas for each of a set of minerals. The compute device, in some embodiments, may include circuitry configured to select one or more models as a function of the obtained parameter data. In some embodiments, the circuitry may be configured such that to select one or more models as a function of the obtained parameter data includes selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, the circuitry is configured such that producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. In some embodiments, the circuitry is configured such that producing at least one prediction includes reformatting the parameter data for use by the one or more models.\|[0008] The circuitry may be configured such that producing at least one prediction includes utilizing one or more machine learning models. Additionally or alternatively, the circuitry may be configured utilize an ensemble of models to produce the at least one prediction. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period. The circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, the circuitry may be configured such that to produce at least one prediction involves producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured per hectare.\|[0009] The circuitry may be configured to produce at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, the circuitry is configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time. The circuitry may be configured such that to produce the at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions.\|[0010] In some embodiments, the circuitry may be configured such that to produce at least one prediction involves determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. The compute device, in some embodiments, may have circuitry configured such that to produce at least one prediction involves determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. In some embodiments, the circuitry may be further configured to determine, from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, the circuitry is configured such that to present a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.\|[0011] According to another aspect of the present disclosure, a method includes obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The method may further include producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. In doing so, the method may include simulating co-precipitation of iron with one or more toxic metals. The method may further include presenting, by the compute device, a visual representation of the at least one prediction in a user interface.\|[0012] In some embodiments, producing, using one or more models from a library of models, at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. Producing, using one or more models from a library of models, at least one prediction may, in some embodiments, include utilizing one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, producing, using one or more models from a library of models, at least one prediction may include utilizing one or more models that simulate co-precipitation of iron with toxic metals. Obtaining parameter data may, in some embodiments, include obtaining data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, obtaining data indicative of properties of soil may include obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and a basalt mineral composition.\|[0013] Obtaining parameter data may include obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. Obtaining parameter data as a function of an identification of the location where the carbon dioxide is to be captured may include reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. Obtaining parameter data may include obtaining parameter data through user input into corresponding fields of a user interface. The method may also include calculating, by the compute device and as a function of the obtained parameter data, additional parameter data for use by the one or more models. Calculating additional parameter data may include calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.\|[0014] In some embodiments, calculating additional parameter data may additionally include utilizing a database of specific surface areas for each of a set of minerals. Producing at least one prediction may include selecting one or more models as a function of the obtained parameter data. Selecting one or more models as a function of the obtained parameter data may involve selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. Producing at least one prediction may include reformatting the parameter data for use by the one or more models. In some embodiments, producing at least one prediction involves utilizing one or more machine learning models. Producing at least one prediction may, in some embodiments, include utilizing an ensemble of models to produce the at least one prediction. Producing at least one prediction may include producing one or more predictions indicative of tons of carbon dioxide captured over a predefined time period.\|[0015] Producing one or more predictions may include producing one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, producing at least one prediction includes producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. Producing one or more predictions may, in some embodiments, include producing one or more predictions indicative of tons of carbon dioxide captured per hectare. In some embodiments, producing at least one prediction includes producing at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. Producing at least one prediction indicative of toxic metal concentrations in water may, in some embodiments, involve producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, producing at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time.\|[0016] Producing the at least one prediction indicative of toxic metal concentrations in water may involve producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, producing the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions. Producing at least one prediction may include determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. In some embodiments, producing at least one prediction includes determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. The method may also include determining, by the compute device and from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, presenting a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.\|[0017] According to another aspect of the present disclosure, one or more machine-readable storage media may include instructions stored thereon that, in response to being executed, cause a compute device to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The instructions may further cause the compute device to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Additionally, the instructions may cause the compute device to present a visual representation of the at least one prediction in a user interface. Further, the instructions may cause the compute device to perform any of the methods described above.\|[0018] Additional features, which alone or in combination with any other feature(s), such as those listed above and/or those listed in the claims, may comprise patentable subject matter and will become apparent to those skilled in the art upon consideration of the following detailed description of various embodiments exemplifying the best mode of carrying out the embodiments as presently perceived.\|(US20260017435)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0019] The concepts described herein are illustrated by way of example and not by way of limitation in the accompanying figures. For simplicity and clarity of illustration, elements illustrated in the figures are not necessarily drawn to scale. Where considered appropriate, reference labels have been repeated among the figures to indicate corresponding or analogous elements. The detailed description particularly refers to the accompanying figures in which:\|[0020] FIG. 1 is a simplified block diagram of at least one embodiment of a system for modeling carbon dioxide removal through enhanced rock weathering;\|[0021] FIG. 2 is a simplified block diagram of at least one embodiment of a compute device of the system of FIG. 1;\|[0022] FIGS. 3-7 are flowcharts of at least one embodiment of a method for modeling carbon dioxide removal through enhanced rock weathering that may be performed by the system of FIG. 1;\|[0023] FIGS. 8 and 9 are user interfaces that may be produced by the system of FIG. 1; and\|[0024] FIG. 10 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating carbon capture as a function of years;\|[0025] FIG. 11 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating a simulation of carbon capture as a function of time;\|[0026] FIG. 12 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating the confidence interval of the simulations over a five year period;\|[0027] FIG. 13 is one embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1; and\|[0028] FIG. 14 is another embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1\|(US20260017435)\|DETAILED DESCRIPTION OF THE DRAWINGS\|[0029] While the concepts of the present disclosure are susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and will be described herein in detail. It should be understood, however, that there is no intent to limit the concepts of the present disclosure to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives consistent with the present disclosure and the appended claims.\|[0030] References in the specification to “one embodiment,” “an embodiment,” “an illustrative embodiment,” etc., indicate that the embodiment described may include a particular feature, structure, or characteristic, but every embodiment may or may not necessarily include that particular feature, structure, or characteristic. Moreover, such phrases are not necessarily referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with an embodiment, it is submitted that it is within the knowledge of one skilled in the art to effect such feature, structure, or characteristic in connection with other embodiments whether or not explicitly described. Additionally, it should be appreciated that items included in a list in the form of “at least one A, B, and C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C). Similarly, items listed in the form of “at least one of A, B, or C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C).\|[0031] The disclosed embodiments may be implemented, in some cases, in hardware, firmware, software, or any combination thereof. The disclosed embodiments may also be implemented as instructions carried by or stored on a transitory or non-transitory machine-readable (e.g., computer-readable) storage medium, which may be read and executed by one or more processors. A machine-readable storage medium may be embodied as any storage device, mechanism, or other physical structure for storing or transmitting information in a form readable by a machine (e.g., a volatile or non-volatile memory, a media disc, or other media device).\|[0032] In the drawings, some structural or method features may be shown in specific arrangements and/or orderings. However, it should be appreciated that such specific arrangements and/or orderings may not be required. Rather, in some embodiments, such features may be arranged in a different manner and/or order than shown in the illustrative figures. Additionally, the inclusion of a structural or method feature in a particular figure is not meant to imply that such feature is required in all embodiments and, in some embodiments, may not be included or may be combined with other features.\|[0033] Referring now to FIG. 1, a system 100 for modeling carbon dioxide removal through enhanced rock weathering includes a set of one or more modeling compute devices 120, a set of source compute devices 140, 142, 144 and a set of target compute devices 150, 152, 154. In operation, the modeling compute devices 120 operate as a gateway 110 through which end users (e.g., scientists, organizations, etc.) of operating target compute devices 150, 152, 154 may view predictions (e.g., forecasts) of how much carbon dioxide will be captured in the soil at a particular location through a process of enhanced rock weathering. In enhanced rock weathering, rock, such as basalt, is added to soil at a location (e.g., one or more hectares of land) in a powdered form to increase the amount of carbon dioxide removed from the atmosphere through interaction between the carbon dioxide, water (e.g., rain), and rock. The composition of the basalt (e.g., mineral composition) as well as properties of the soil itself (e.g., porosity, carbon content, minerals, etc.) influence the amount of carbon dioxide that will be captured and may impact an amount of toxic metals present in the soil and/or water in the location as a result of the chemical processes involved in the capture of the carbon dioxide. As such, given the multitude of factors that can influence the amount of carbon dioxide removal, the modeling compute devices 120 may utilize a library of models 130 (e.g., thousands of models) and a database 132 of properties of minerals that also affect the amount of carbon dioxide that will be captured. The modeling compute devices 120 produce results 134, which may be embodied as data indicative of amount of carbon dioxide that will be captured under the specified conditions. Additionally, the results 134 may indicate the amount of toxic metals that are predicted to be present in the soil and water as a result of the chemical processes. Further, the results may be broken down across multiple years, depths, confidence intervals, or other parameters and may be the product of thousands of simulations using the set of models 130.\|[0034] The source compute devices 140, 142, 144 may provide data indicative of properties of the soil in various locations, properties of basalt (e.g., various feed stocks of basalt), information indicative of a carbon credits market (e.g., an amount of carbon credits associated with an amount of carbon captured or removed from the atmosphere), data indicative of regulations associated with various locations (e.g., drinking water regulations, irrigation water regulations, soil regulations), and/or other data usable by the modeling compute devices 120 in simulating the capture of carbon from the atmosphere through enhanced rock weathering processes.\|[0035] In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. The system 100, in operation, provides innovative and independent geochemical models and modeling forecasts, filling a current gap in monitoring, reporting, and verification (MRV). Further, the system 100 contributes to the trust that is necessary for the scale-up of climate-tech carbon dioxide removal (CDR) industries to the gigaton level. While the system 100, in some embodiments, focuses on enhanced rock weathering, the science and technologies can also be applied to storing carbon dioxide in basalt and sandstone aquifers and mine tailings.\|[0036] A modeling forecast is useful at every stage of a project: conceptualization, contract negotiation, application, and post-project monitoring. The gateway 110, in the illustrative embodiment, is cloud-based, documented, and based on advanced cyberinfrastructure and data sciences that transform how modeling is delivered and how results are archived, analyzed, and presented. The gateway 110, in the illustrative embodiment, provides industry-standard authentication, authorization, and controlled sharing capabilities. Further, the system 100 provides provenance for the execution of tools, clonability, and reusability and integrates with national open cyberinfrastructure and public clouds for workflow execution.\|[0037] In the illustrative embodiment, the gateway 110 may serve four types of clients: a) technical specialists at stakeholders (CDR and purchaser corporations, regulatory agencies, environmental groups) who can search a large library of models 130 to find the likely outcomes for their projects; b) geochemical experts who can develop or tweak their models 130 on the gateway 110, but aided by automatic documentation, archives, and traceability on the gateway; c) stakeholders with no in-house capabilities who wish to outsource the initial development of models 130 and run the models 130 on the gateway 110; d) stakeholders who need independent models as certification. The availability of the gateway 110 may operate to broaden the participation of underrepresented groups and less developed countries, helping achieve the common goal of implementing scalable solutions around the world.\|[0038] Enhanced rock weathering can be generally represented with the equations shown below:\|[0039] Other equations representative of geochemical reactions are set forth in “Environmental Applications of Geochemical Modeling” by Chen Zhu and Greg Anderson, published in 2002, the contents of which are incorporated herein by reference. As discussed herein, characteristics of the soil and basalt in the soil can significantly impact the amount of carbon dioxide that will be captured and the amounts of metals (e.g., toxic metals) that may be introduced into the soil and water through the enhanced rock wreathing process. The models 130, in the illustrative embodiment, account for the characteristics through parameters discussed herein. Further, the models 130 incorporate features that are not present in conventional modeling systems, including the following: a. Near-equilibrium rates (e.g., in systems with relatively low Gibbs energy) are modeled to be one to two orders of magnitude slower than the far-from-equilibrium rates (e.g., in systems with relatively high Gibbs energy), rather than the far-from-equilibrium rate constants used in other models; b. basalt weathering is simulated as irreversible reactions with unidirectional rates (not reversible reactions in other models, which are theoretically wrong); and c. the models 130 include co-precipitation of toxic metals released from enhanced rock weathering with iron oxyhydroxides. Without co-precipitation in the models 130, the forecasts of toxic metal released into soil may incorrectly indicate toxic metal amounts in excess of applicable regulations. The models 130 may be fine-tuned with time, and more components may be added to the model 130.\|[0040] Further, the system 100, in the illustrative embodiment, provides a web-based model interface. Geochemical models are generally inaccessible to non-experts and the number of experts in the world is in short supply. The system 100 leverages expertise and experience of experts and makes modeling and modeling results available to non-experts. The gateway 110, in the illustrative embodiment, utilizes a database (e.g., the database 132) of mineralogical compositions of basalt feed stocks to be applied to croplands, and provides a web tool (e.g., a web based user interface) that allows users to input mineralogical compositions of the specific feed stock. Behind the web interface, the gateway 110 utilizes a database (e.g., the database 132) of different specific surface areas for different minerals. In operation, the gateway 110 may perform automatic input file generation (e.g., reformatting of parameter data into a format usable by the models 130).\|[0041] The web interface and models enable users (e.g., operating the target compute devices 150, 152, 154) to combine different parameters and run different scenarios to view resulting predictions of carbon capture through enhanced rock weathering and side effects thereof. For example, users may compare how much carbon dioxide is captured by applying 100 tons of basalt per hectare versus ten tons of basalt per hectare, and using one feed stock of basalt (e.g., Oregon basalt) versus another feed stock of basalt (e.g., Columbia River basalt). Users may also view the differences in carbon capture given different particle sizes. Further, users may view data that is indicative of toxic metal release into water and soil under varying conditions.\|[0042] In the illustrative embodiment, the gateway 110 may maintain a library of millions of simulations with a wide range of field conditions. The library may be searchable and the gateway 110 may enable users to locate modeling results and graphic presentations that fit their field conditions within minutes, rather than waiting for hours or longer for simulation results. The library may serve as a base for development or improvement of machine learning algorithms to (1) accelerate the simulations; and (2) find patterns, which lead to faster, more accurate, and more interpretable models. The models 130, in the illustrate embodiment, are calibrated geochemical models that bridge the gap between laboratory and field-based estimates of geochemical reactions. In particular, the models 130 may be calibrated with enhanced rock weathering batch scale laboratory experimental data, field data, and lysimeter experimental data. The results 134 may be embodied as databases and input files with adjusted parameters or semi-empirical scaling factors. In effect, the gateway 110 may provide independent, rigorous, models and modeling results that come with trust and creditability.\|[0043] While a relatively small number of compute devices 120, 140, 142, 144, 150, 152, 154 are shown in FIG. 1 for simplicity and clarity, it should be understood that the number of compute devices, in practice, may range in the tens, hundreds, thousands, or more. Likewise, it should be understood that the compute devices 120, 140, 142, 144, 150, 152, 154 may be distributed differently or perform different roles than the configuration shown in FIG. 1. Further, though shown as separate compute devices 120, 140, 142, 144, 150, 152, 154 in some embodiments, the functionality of one or more of the compute devices 120, 140, 142, 144, 150, 152, 154 may be combined into fewer compute devices and/or distributed across more compute devices than those shown in FIG. 1.\|[0044] Referring now to FIG. 2, an illustrative embodiment of a modeling compute device 120 includes a compute engine 210, an input/output (I/O) subsystem 216, communication circuitry 218, and one or more data storage devices 222. In some embodiments, the modeling compute device 120 may include one or more display devices 224 and/or one or more peripheral devices 226 (e.g., a mouse, a physical keyboard, etc.). In some embodiments, one or more of the illustrative components may be incorporated in, or otherwise form a portion of, another component. The compute engine 210 may be embodied as any type of device or collection of devices capable of performing various compute functions described below. In some embodiments, the compute engine 210 may be embodied as a single device such as an integrated circuit, an embedded system, a field-programmable gate array (FPGA), a system-on-a-chip (SOC), or other integrated system or device. Additionally, in the illustrative embodiment, the compute engine 210 includes or is embodied as a processor 212 and a memory 214. The processor 212 may be embodied as any type of processor capable of performing the functions described herein. For example, the processor 212 may be embodied as a single or multi-core processor(s), a microcontroller, or other processor or processing/controlling circuit. In some embodiments, the processor 212 may be embodied as, include, or be coupled to an FPGA, an application specific integrated circuit (ASIC), reconfigurable hardware or hardware circuitry, or other specialized hardware to facilitate performance of the functions described herein.\|[0045] In embodiments, the processor 212 is capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, a set of instructions which when executed by the processor 212 cause the modeling compute device 120 to perform one or more operations described herein. In embodiments, the processor 212 is further capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, one or more signals from external sources, e.g., from the peripheral devices 226 or via the communication circuitry 218 from an external compute device, external source, or external network. As one will appreciate, a signal may contain encoded instructions and/or information. In embodiments, once received, such a signal may first be stored, e.g., in the memory 214 or in the data storage device(s) 222, thereby allowing for a time delay in the receipt by the processor 212 before the processor 212 operates on a received signal. Likewise, the processor 212 may generate one or more output signals, which may be transmitted to an external device, e.g., an external memory or an external compute engine via the communication circuitry 218 or, e.g., to one or more display devices 224. In some embodiments, a signal may be subjected to a time shift in order to delay the signal. For example, a signal may be stored on one or more storage devices 222 to allow for a time shift prior to transmitting the signal to an external device. One will appreciate that the form of a particular signal will be determined by the particular encoding a signal is subject to at any point in its transmission (e.g., a signal stored will have a different encoding than a signal in transit, or, e.g., an analog signal will differ in form from a digital version of the signal prior to an analog-to-digital (A/D) conversion).\|[0046] The main memory 214 may be embodied as any type of volatile (e.g., dynamic random access memory (DRAM), etc.) or non-volatile memory or data storage capable of performing the functions described herein. Volatile memory may be a storage medium that requires power to maintain the state of data stored by the medium. In some embodiments, all or a portion of the main memory 214 may be integrated into the processor 212. In operation, the main memory 214 may store various software and data used during operation such as models, databases, simulation results, applications, libraries, and drivers.\|[0047] The compute engine 210 is communicatively coupled to other components of the modeling compute device 120 via the I/O subsystem 216, which may be embodied as circuitry and/or components to facilitate input/output operations with the compute engine 210 (e.g., with the processor 212 and the main memory 214) and other components of the modeling compute device 120. For example, the I/O subsystem 216 may be embodied as, or otherwise include, memory controller hubs, input/output control hubs, integrated sensor hubs, firmware devices, communication links (e.g., point-to-point links, bus links, wires, cables, light guides, printed circuit board traces, etc.), and/or other components and subsystems to facilitate the input/output operations. In some embodiments, the I/O subsystem 216 may form a portion of a system-on-a-chip (SoC) and be incorporated, along with one or more of the processor 212, the main memory 214, and other components of the modeling compute device 120, into the compute engine 210.\|[0048] The communication circuitry 218 may be embodied as any communication circuit, device, or collection thereof, capable of enabling communications over a network between the modeling compute device 120 and another device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). The communication circuitry 218 may be configured to use any one or more communication technology (e.g., wired or wireless communications) and associated protocols (e.g., Ethernet, Wi-Fi®, WiMAX, Bluetooth®, etc.) to effect such communication.\|[0049] The illustrative communication circuitry 218 includes a network interface controller (NIC) 220. The NIC 220 may be embodied as one or more add-in-boards, daughter cards, network interface cards, controller chips, chipsets, or other devices that may be used by the modeling compute device 120 to connect with another compute device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). In some embodiments, the NIC 220 may be embodied as part of a system-on-a-chip (SoC) that includes one or more processors, or included on a multichip package that also contains one or more processors. In some embodiments, the NIC 220 may include a local processor (not shown) and/or a local memory (not shown) that are both local to the NIC 220. Additionally or alternatively, in such embodiments, the local memory of the NIC 220 may be integrated into one or more components of the modeling compute device 120 at the board level, socket level, chip level, and/or other levels.\|[0050] Each data storage device 222, may be embodied as any type of device configured for short-term or long-term storage of data such as, for example, memory devices and circuits, memory cards, hard disk drives, solid-state drives, or other data storage device. Each data storage device 222 may include a system partition that stores data and firmware code for the data storage device 222 and one or more operating system partitions that store data files and executables for operating systems.\|[0051] Each display device 224 may be embodied as any device or circuitry (e.g., a liquid crystal display (LCD), a light emitting diode (LED) display, a cathode ray tube (CRT) display, etc.) configured to display visual information (e.g., text, graphics, etc.) to a user. In some embodiments, a display device 224 may be embodied as a touch screen (e.g., a screen incorporating resistive touchscreen sensors, capacitive touchscreen sensors, surface acoustic wave (SAW) touchscreen sensors, infrared touchscreen sensors, optical imaging touchscreen sensors, acoustic touchscreen sensors, and/or other type of touchscreen sensors) to detect selections of on-screen user interface elements or gestures from a user.\|[0052] In the illustrative embodiment, the components of the modeling compute device 120 are housed in a single unit. However, in other embodiments, the components may be in separate housings, in separate racks of a data center, and/or spread across multiple data centers or other facilities. The compute devices 140, 142, 144, 150, 152, 154 may have components similar to those described in FIG. 2 with reference to the modeling compute device 120. The description of those components of the modeling compute device 120 is equally applicable to the description of components of the compute devices 140, 142, 144, 150, 152, 154. Further, it should be appreciated that any of the devices 120, 140, 142, 144, 150, 152, 154 may include other components, sub-components, and devices commonly found in a computing device, which are not discussed above in reference to the modeling compute device 120 and not discussed herein for clarity of the description.\|[0053] In the illustrative embodiment, the compute devices 120, 140, 142, 144, 150, 152, 154 are in communication via a network 160, which may be embodied as any type of wired or wireless communication network, including global networks (e.g., the internet), wide area networks (WANs), local area networks (LANs), digital subscriber line (DSL) networks, cable networks (e.g., coaxial networks, fiber networks, etc.), cellular networks (e.g., Global System for Mobile Communications (GSM), Long Term Evolution (LTE), Worldwide Interoperability for Microwave Access (WiMAX), 3G, 4G, 5G, etc.), a radio area network (RAN), or any combination thereof.\|[0054] Referring now to FIG. 3, the system 100 (e.g., a modeling compute device 120 of the gateway 110) may perform a method 300 for modeling carbon dioxide removal through enhanced rock weathering. The method 300, in the illustrative embodiment, begins with block 302 in which the modeling compute device 120 obtains parameter data indicative of parameters for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering (e.g., the application of basalt dust to soil to increase the amount of carbon dioxide captured through the interaction of water (e.g., rain), carbon dioxide, and rock (e.g., the basalt dust)). In doing so, and as indicated in block 304, the modeling compute device 120 obtains data indicative of properties of soil in a location where the carbon dioxide is to be captured (e.g., removed from the atmosphere through enhanced rock weathering). In the illustrative embodiment, the modeling compute device 120 may obtain data indicative of minerals in the soil (e.g., a numeric value, such as a number indicative of a percentage of the soil comprising minerals), as indicated in block 306. As indicated in block 308, the modeling compute device 120 may obtain data indicative of carbon in the soil (e.g., a numeric value indicative of a percentage of the soil comprising carbon).\|[0055] The modeling compute device 120 may additionally obtain data indicative of effective porosity of the soil where the carbon is to be captured, as indicated in block 310. The effective porosity may be expressed, in at least some embodiments, as a numeric value (e.g., a percentage). As indicated in block 312, the modeling compute device 120 may obtain parameter data indicative of total specific surface area. In at least some embodiments, the total specific surface area may be expressed as square meters per gram. The modeling compute device 120 may obtain data indicative of the height of a top soil layer, as indicated in block 314. The height, in the illustrative embodiment, is expressed in meters. Further, the modeling compute device 120 may obtain data indicative of an amount of basalt added to the soil (e.g., tons per hectare), as indicated in block 316. Further, the modeling compute device 120 may obtain data indicative of basalt density, such as in grams per cubic centimeter, as indicated in block 318. Additionally, the modeling compute device 120 may obtain data indicative of bulk soil density, as indicated in block 320. The bulk soil density, in at least some embodiments, may be expressed as grams per cubic centimeter. The modeling compute device 120 may also obtain data indicative of basalt mineral composition, as indicated in block 322. The mineral composition of the basalt may be structured as one or more pairs of values, with each pair including an identifier (e.g., name, abbreviation, etc.) of a mineral and a corresponding percentage (e.g., indicative of a percentage of the basalt feed stock that the mineral constitutes).\|[0056] Still referring to FIG. 3, the modeling compute device 120 may obtain the parameter data as a function of (e.g., based on) an identification of the location where the carbon dioxide is to be captured in the soil, as indicated in block 324. In doing so, the modeling compute device 120 may read parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of properties of soil associated with location identifiers (e.g., plot numbers, geographic coordinates, zip codes, etc.), as indicated in block 326. In some embodiments, the modeling compute device 120 may obtain parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of mineral compositions from each of multiple basalt feed stocks, as indicated in block 328. Additionally or alternatively, the modeling compute device 120 may obtain parameter data through user input into corresponding fields (e.g., text boxes, check boxes, etc.) of a user interface (e.g., a graphical user interface presented by a target compute device 150, 152, 154 based on code (e.g., hypertext markup language (HTML) and/or JavaScript) and images (e.g., portable network graphics (PNG) files, Joint Photographic Experts Group (JPEG) files, or the like) transmitted from the modeling compute device 120 to the target compute device(s) 150, 152, 154 via the network 160, as indicated in block 330. An embodiment of a user interface 800 with which the modeling compute device 120 may obtain parameter data is shown in FIG. 8. The user interface 800 includes a first screen 810 that comprises parameter data about soil properties and a second screen 820 that includes parameter data about basalt mineral makeup. The user interface 800 provides one embodiment that users can use to input parameters related to soil properties and basalt mineral composition, run the models, and calculate how much CO2 can be sequestered.\|[0057] Referring now to FIG. 4, the method 300 continues in block 332 in which the modeling compute device 120 may calculate, as a function of the obtained parameter data, additional parameter data for use by one or more models (e.g., the models 130). In doing so, the modeling compute device 120 may calculate air and blind pores (e.g., a numeric value), as indicated in block 334. The modeling compute device 120 may additionally calculate a volume of soil per hectare, as indicated in block 336. Further, the modeling compute device 120 may calculate a number of volume (e.g., liters) of pore water per unit of area (e.g., hectare), as indicated in block 338. Additionally, the modeling compute device 120 may calculate a mass of basalt per unit of volume of the soil, as indicated in block 340. In addition, the modeling compute device 120 may calculate a concentration of basalt in the soil, as indicated in block 342. Further, the modeling compute device 120 may calculate a total weight percentage, as indicated in block 344. The modeling compute device 120 may also calculate a rock specific surface area, as indicated in block 346. In addition, the modeling compute device 120 may calculate a total surface area, in block 348. In performing the calculations, the modeling compute device 120 may utilize a database (e.g., a database 132) of specific surface areas for each of a set of minerals (e.g., minerals in the soil, in the basalt, etc.), as indicated in block 350. An embodiment of a user interface 900 in which the modeling compute device 120 may display additional parameters calculated as discussed above is shown in FIG. 9. In some embodiments, the user interface 800 includes a third screen 830 that may display additional parameters calculated as discussed above.\|[0058] After obtaining the parameter data, the method 300, in the illustrative embodiment, advances to block 352, in which the modeling compute device 120 produces, using one or models from a library of models (e.g., the models 130), one or more predictions indicative of an amount of carbon dioxide that will be removed from the atmosphere (e.g., captured through enhanced rock weathering). In doing so, the modeling compute device 120 may select one or more models 130 as a function of the obtained parameter data, as indicated in block 354. That is, the modeling compute device 120 may select one or more models 130 from the library of models as a function of a determined similarity (e.g., a similarity score, such as a calculated distance (e.g., a Euclidean distance, a cosine similarity, a result of a clustering analysis, etc.)) of the parameter data (e.g., obtained in block 302) to reference parameters for which one or more corresponding models 130 have been identified (e.g., in a data set in the memory 214 or storage 222, in a database 132, etc.) as having a high accuracy of predictions (e.g., the results 134 produced by those models have been shown to predict within a predefined threshold of accuracy (e.g., a defined percentage), actual results that were later measured in field tests). That is, if a particular model 130 is identified as more accurately predicting the amount of carbon dioxide that will be removed from the atmosphere than other models, when the parameters are similar to those obtained in block 302, the modeling compute device 120 may select that model for use.\|[0059] In some embodiments, as indicated in block 358, the modeling compute device 120 may select one or more models 130 as a function of a distance of the location where the carbon dioxide is to be captured to each of a set of reference locations associated with the models 130. That is, a data set (e.g., in the memory 214, the data storage 222, or a database 132) may identify a location (e.g., a zip code, a set of geographic coordinates, or other identifier of a location) with each model 130 in the library (e.g., because the corresponding model 130 has been shown to produce predictions with high accuracy for the associated location) and the modeling compute device 120 may select a set (e.g., one or more) of the models 130 that are closest to the location where the carbon dioxide is to be captured.\|[0060] Referring now to FIG. 5, in block 360, the modeling compute device 120 may reformat the parameter data for use by the models 130 (e.g., by converting the data into a file format that the models 130 are configured to parse (e.g., using a scripting language such as Python)). As indicated in block 362, the modeling compute device 120 may select one or more machine learning models (e.g., models, such as neural networks, decision trees, or others that may iteratively improve in prediction accuracy based on feedback). In some embodiments, the modeling compute device 120 may select an ensemble (e.g., a combination of models, in which outputs of the individual models may be weighted relative to each other), as indicated in block 364. The models 130 may include one or more models implemented by PHREEQC (e.g., PHREEQC 3), from the U.S. Geological Survey, GEM (e.g., reservoir modeling), TOUGHREACT from Lawrence Berkeley National Laboratory, and/or other models (e.g., provided by entities associated with one or more of the source compute devices 140, 142, 144). The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period, as indicated in block 366. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured each year of a defined number of years at the specified location, as indicated in block 368.\|[0061] The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per unit of area, as indicated in block 370. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per hectare, as indicated in block 372. In the illustrative embodiment, and unlike conventional systems, the modeling compute device 120 utilizes models that simulate co-precipitation of iron with toxic metals, as indicated in block 374. Additionally, and unlike conventional systems, the modeling compute device 120, in the illustrative embodiment, utilizes models that simulate basalt weathering as irreversible reactions with unidirectional rates, as indicated in block 376. Further, and unlike conventional systems, the modeling compute device 120 in the illustrative embodiment utilizes models in which near-equilibrium (e.g., within a defined percentage of an equilibrium state) rates are one to two orders of magnitude slower than far-from-equilibrium (e.g., not within the defined percentage of the equilibrium state) rates, as indicated in block 378. Further, and as indicated in block 380, the modeling compute device 120, in the illustrative embodiment, produces one or more predictions indicative of toxic metal concentrations in water associated with the location where the carbon dioxide is to be captured. In doing so, the modeling compute device 120 may produce one or more predictions indicative of concentrations of Nickel, Chromium, and/or Cadmium in the water, as indicated in block 382.\|[0062] Referring now to FIG. 6, the modeling compute device 120 may produce the one or more predications as a function of depth (e.g., depth of the water), as indicated in block 384. As indicated in block 386, the modeling compute device 120 may produce the one or more predictions regarding toxic metals in the water as a function of time (e.g., amount of toxic metals in the water per year). In some embodiments, the modeling compute device 120 may produce the predictions of toxic metals in the water relative to one or more regulations associated with the location where the carbon dioxide is to be captured, as indicated in block 388. That is, the modeling compute device 120 may obtain data (e.g., from a database 132, from a source compute device 140, 142, 144) indicative of applicable regulations and indicate whether the predicted amount of toxic metals satisfies (e.g., does not violate the regulation(s), is close to (e.g., within a defined percentage of), etc.) a limit specified by the regulations. The modeling compute device 120 may produce the prediction(s) relative to drinking water regulations and/or irrigation water regulations, as indicated in blocks 390, 392. The modeling compute device 120 may produce one or more predictions indicative of toxic metal concentrations in the soil associated with the location where the carbon dioxide is to be captured, as indicated in block 394. In doing so, the modeling compute device 120 may produce prediction(s) indicative of concentrations of Nickel, Chromium, and/or Cadmium in the soil, as indicated in block 396. The modeling compute device 120 may produce the prediction(s) as a function of depth (e.g., in the soil) and/or as a function of time, as indicated in blocks 398, 400. Similar to block 388, the modeling compute device 120 may produce the prediction(s) of toxic metals in the soil relative to one or more regulations associated with the location, as indicated in block 402.\|[0063] Referring now to FIG. 7, the modeling compute device 120 may produce data indicative of probabilities (e.g., confidence) associated with the one or more predictions, as indicated in block 404. For example, the modeling compute device 120 may produce a predictions as confidence intervals, with one prediction associated with a particular level of confidence (e.g., a percentage of likelihood), and one or more other predictions associated with other levels of confidence. As indicated in block 406, the modeling compute device 120 may determine an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. For example, the modeling compute device 120 may obtain data (e.g., from a source compute device 140, 142, 144, a database 132, etc.) indicative of a conversion rate between tons of carbon captured and a number of corresponding carbon credits and multiply the predicted amount of carbon dioxide by the conversion rate to determine the amount of carbon credits. In some embodiments, the modeling compute device 120 may adjust the number of carbon credits based on a probability or confidence level associated with the predicted amount of carbon dioxide to be removed from block 404 (e.g., by multiplying the amount of carbon dioxide by a percentage associated with the probability or confidence level). As indicated in block 408, the modeling compute device 120 may determine soil parameters that will increase capture of carbon dioxide at the location. For example, and as indicated in block 410, the modeling compute device 120 may determine, from a set of multiple basalt feed stocks, each having different mineral compositions and/or other properties, a basalt feed stock predicted to capture the most carbon dioxide in the location while maintaining compliance with regulations (e.g., toxic metals in the soil, toxic metals in the water). The modeling compute device 120 may do so by simulating carbon dioxide capture with each of the basalt feed stocks using the models 130 and identifying the basalt feed stock that satisfies the above conditions to the greatest degree.\|[0064] Continuing the method 300, the modeling compute device 120 may present a visual representation of the one or more prediction(s) in a user interface, as indicated in block 412. In the illustrative embodiment, the modeling compute device 120 produces visual presentation(s) of the prediction(s) in a web based interface (e.g., based on a HTML, JavaScript, and image data sent from the modeling compute device 120 to one or more rending engines (e.g., web browser(s)) executed by corresponding target compute devices 150, 152, 154). As indicated in block 416, in producing one or more visual representations of the prediction(s), the modeling compute device 120 may present visual representations that include interactive graphs (e.g., in which time periods, depths, or other parameters may be selected and a corresponding graph is presented). Example embodiments of visual representations 1000, 1100, 1200, 1300, 1400 of the predictions that may be presented by the modeling compute device 120 and displayed by one or more of the corresponding target compute devices 150, 152, 154 are shown in FIGS. 10-14.\|[0065] While certain illustrative embodiments have been described in detail in the drawings and the foregoing description, such an illustration and description is to be considered as exemplary and not restrictive in character, it being understood that only illustrative embodiments have been shown and described and that all changes and modifications that come within the spirit of the disclosure are desired to be protected. There exists a plurality of advantages of the present disclosure arising from the various features of the apparatus, systems, and methods described herein. It will be noted that alternative embodiments of the apparatus, systems, and methods of the present disclosure may not include all of the features described, yet still benefit from at least some of the advantages of such features. Those of ordinary skill in the art may readily devise their own implementations of the apparatus, systems, and methods that incorporate one or more of the features of the present disclosure.	(US20260017435)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/669,351 filed on Jul. 10, 2024, the disclosure of which is expressly incorporated herein.\|(US20260017435)\|BACKGROUND\|[0002] Climate change is a growing concern across the world as atmospheric greenhouse gases such as carbon dioxide trap energy radiated from the sun. While a direct result of increases in greenhouse gases is increased temperatures on Earth, knock on effects include droughts, flooding, loss of biodiversity, and disruptions in energy and transportation systems across the world. Through interactions between water and rock (e.g., in soil), carbon dioxide can be captured (e.g., removed) from the atmosphere and correspondingly lessen the effects of climate change. However, given the multitude of factors that influence the complex interactions between water and rock, it is not feasible in conventional computerized systems to reliably determine the amount of carbon dioxide that will be removed in a given location, under a given set of conditions, or to predict side effects of any efforts to enhance the capture of carbon dioxide in the soil. Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.\|SUMMARY\|[0003] The present application discloses one or more of the features recited in the appended claims and/or the following features which, alone or in any combination, may comprise patentable subject matter:\|[0004] According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may be further configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. Producing a prediction may include simulating co-precipitation of iron with one or more toxic metals. The circuitry may be further configured to present a visual representation of the at least one prediction in a user interface.\|[0005] In some embodiments, the circuitry may be configured such that using one or more models from a library of models to produce at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. The circuitry may also be configured to utilize one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, the circuitry may be configured to utilize one or more models that simulate co-precipitation of iron with toxic metals. The circuitry may be configured to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that obtaining data indicative of properties of soil includes obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and basalt mineral composition.\|[0006] The circuitry may be configured such that obtaining parameter data includes obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured to obtain parameter data as a function of an identification of the location where the carbon dioxide is to be captured by reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. The circuitry may be configured to obtain parameter data through user input into corresponding fields of a user interface. In some embodiments, the circuitry may be further configured to calculate, as a function of the obtained parameter data, additional parameter data for use by the one or more models. The circuitry may be configured such that calculating additional parameter data involves calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.\|[0007] In some embodiments, calculating additional parameter data further includes utilizing a database of specific surface areas for each of a set of minerals. The compute device, in some embodiments, may include circuitry configured to select one or more models as a function of the obtained parameter data. In some embodiments, the circuitry may be configured such that to select one or more models as a function of the obtained parameter data includes selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, the circuitry is configured such that producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. In some embodiments, the circuitry is configured such that producing at least one prediction includes reformatting the parameter data for use by the one or more models.\|[0008] The circuitry may be configured such that producing at least one prediction includes utilizing one or more machine learning models. Additionally or alternatively, the circuitry may be configured utilize an ensemble of models to produce the at least one prediction. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period. The circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, the circuitry may be configured such that to produce at least one prediction involves producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured per hectare.\|[0009] The circuitry may be configured to produce at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, the circuitry is configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time. The circuitry may be configured such that to produce the at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions.\|[0010] In some embodiments, the circuitry may be configured such that to produce at least one prediction involves determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. The compute device, in some embodiments, may have circuitry configured such that to produce at least one prediction involves determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. In some embodiments, the circuitry may be further configured to determine, from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, the circuitry is configured such that to present a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.\|[0011] According to another aspect of the present disclosure, a method includes obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The method may further include producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. In doing so, the method may include simulating co-precipitation of iron with one or more toxic metals. The method may further include presenting, by the compute device, a visual representation of the at least one prediction in a user interface.\|[0012] In some embodiments, producing, using one or more models from a library of models, at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. Producing, using one or more models from a library of models, at least one prediction may, in some embodiments, include utilizing one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, producing, using one or more models from a library of models, at least one prediction may include utilizing one or more models that simulate co-precipitation of iron with toxic metals. Obtaining parameter data may, in some embodiments, include obtaining data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, obtaining data indicative of properties of soil may include obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and a basalt mineral composition.\|[0013] Obtaining parameter data may include obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. Obtaining parameter data as a function of an identification of the location where the carbon dioxide is to be captured may include reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. Obtaining parameter data may include obtaining parameter data through user input into corresponding fields of a user interface. The method may also include calculating, by the compute device and as a function of the obtained parameter data, additional parameter data for use by the one or more models. Calculating additional parameter data may include calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.\|[0014] In some embodiments, calculating additional parameter data may additionally include utilizing a database of specific surface areas for each of a set of minerals. Producing at least one prediction may include selecting one or more models as a function of the obtained parameter data. Selecting one or more models as a function of the obtained parameter data may involve selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. Producing at least one prediction may include reformatting the parameter data for use by the one or more models. In some embodiments, producing at least one prediction involves utilizing one or more machine learning models. Producing at least one prediction may, in some embodiments, include utilizing an ensemble of models to produce the at least one prediction. Producing at least one prediction may include producing one or more predictions indicative of tons of carbon dioxide captured over a predefined time period.\|[0015] Producing one or more predictions may include producing one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, producing at least one prediction includes producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. Producing one or more predictions may, in some embodiments, include producing one or more predictions indicative of tons of carbon dioxide captured per hectare. In some embodiments, producing at least one prediction includes producing at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. Producing at least one prediction indicative of toxic metal concentrations in water may, in some embodiments, involve producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, producing at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time.\|[0016] Producing the at least one prediction indicative of toxic metal concentrations in water may involve producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, producing the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions. Producing at least one prediction may include determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. In some embodiments, producing at least one prediction includes determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. The method may also include determining, by the compute device and from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, presenting a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.\|[0017] According to another aspect of the present disclosure, one or more machine-readable storage media may include instructions stored thereon that, in response to being executed, cause a compute device to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The instructions may further cause the compute device to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Additionally, the instructions may cause the compute device to present a visual representation of the at least one prediction in a user interface. Further, the instructions may cause the compute device to perform any of the methods described above.\|[0018] Additional features, which alone or in combination with any other feature(s), such as those listed above and/or those listed in the claims, may comprise patentable subject matter and will become apparent to those skilled in the art upon consideration of the following detailed description of various embodiments exemplifying the best mode of carrying out the embodiments as presently perceived.\|(US20260017435)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0019] The concepts described herein are illustrated by way of example and not by way of limitation in the accompanying figures. For simplicity and clarity of illustration, elements illustrated in the figures are not necessarily drawn to scale. Where considered appropriate, reference labels have been repeated among the figures to indicate corresponding or analogous elements. The detailed description particularly refers to the accompanying figures in which:\|[0020] FIG. 1 is a simplified block diagram of at least one embodiment of a system for modeling carbon dioxide removal through enhanced rock weathering;\|[0021] FIG. 2 is a simplified block diagram of at least one embodiment of a compute device of the system of FIG. 1;\|[0022] FIGS. 3-7 are flowcharts of at least one embodiment of a method for modeling carbon dioxide removal through enhanced rock weathering that may be performed by the system of FIG. 1;\|[0023] FIGS. 8 and 9 are user interfaces that may be produced by the system of FIG. 1; and\|[0024] FIG. 10 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating carbon capture as a function of years;\|[0025] FIG. 11 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating a simulation of carbon capture as a function of time;\|[0026] FIG. 12 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating the confidence interval of the simulations over a five year period;\|[0027] FIG. 13 is one embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1; and\|[0028] FIG. 14 is another embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1;\|(US20260017435)\|DETAILED DESCRIPTION OF THE DRAWINGS\|[0029] While the concepts of the present disclosure are susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and will be described herein in detail. It should be understood, however, that there is no intent to limit the concepts of the present disclosure to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives consistent with the present disclosure and the appended claims.\|[0030] References in the specification to “one embodiment,” “an embodiment,” “an illustrative embodiment,” etc., indicate that the embodiment described may include a particular feature, structure, or characteristic, but every embodiment may or may not necessarily include that particular feature, structure, or characteristic. Moreover, such phrases are not necessarily referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with an embodiment, it is submitted that it is within the knowledge of one skilled in the art to effect such feature, structure, or characteristic in connection with other embodiments whether or not explicitly described. Additionally, it should be appreciated that items included in a list in the form of “at least one A, B, and C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C). Similarly, items listed in the form of “at least one of A, B, or C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C).\|[0031] The disclosed embodiments may be implemented, in some cases, in hardware, firmware, software, or any combination thereof. The disclosed embodiments may also be implemented as instructions carried by or stored on a transitory or non-transitory machine-readable (e.g., computer-readable) storage medium, which may be read and executed by one or more processors. A machine-readable storage medium may be embodied as any storage device, mechanism, or other physical structure for storing or transmitting information in a form readable by a machine (e.g., a volatile or non-volatile memory, a media disc, or other media device).\|[0032] In the drawings, some structural or method features may be shown in specific arrangements and/or orderings. However, it should be appreciated that such specific arrangements and/or orderings may not be required. Rather, in some embodiments, such features may be arranged in a different manner and/or order than shown in the illustrative figures. Additionally, the inclusion of a structural or method feature in a particular figure is not meant to imply that such feature is required in all embodiments and, in some embodiments, may not be included or may be combined with other features.\|[0033] Referring now to FIG. 1, a system 100 for modeling carbon dioxide removal through enhanced rock weathering includes a set of one or more modeling compute devices 120, a set of source compute devices 140, 142, 144 and a set of target compute devices 150, 152, 154. In operation, the modeling compute devices 120 operate as a gateway 110 through which end users (e.g., scientists, organizations, etc.) of operating target compute devices 150, 152, 154 may view predictions (e.g., forecasts) of how much carbon dioxide will be captured in the soil at a particular location through a process of enhanced rock weathering. In enhanced rock weathering, rock, such as basalt, is added to soil at a location (e.g., one or more hectares of land) in a powdered form to increase the amount of carbon dioxide removed from the atmosphere through interaction between the carbon dioxide, water (e.g., rain), and rock. The composition of the basalt (e.g., mineral composition) as well as properties of the soil itself (e.g., porosity, carbon content, minerals, etc.) influence the amount of carbon dioxide that will be captured and may impact an amount of toxic metals present in the soil and/or water in the location as a result of the chemical processes involved in the capture of the carbon dioxide. As such, given the multitude of factors that can influence the amount of carbon dioxide removal, the modeling compute devices 120 may utilize a library of models 130 (e.g., thousands of models) and a database 132 of properties of minerals that also affect the amount of carbon dioxide that will be captured. The modeling compute devices 120 produce results 134, which may be embodied as data indicative of amount of carbon dioxide that will be captured under the specified conditions. Additionally, the results 134 may indicate the amount of toxic metals that are predicted to be present in the soil and water as a result of the chemical processes. Further, the results may be broken down across multiple years, depths, confidence intervals, or other parameters and may be the product of thousands of simulations using the set of models 130.\|[0034] The source compute devices 140, 142, 144 may provide data indicative of properties of the soil in various locations, properties of basalt (e.g., various feed stocks of basalt), information indicative of a carbon credits market (e.g., an amount of carbon credits associated with an amount of carbon captured or removed from the atmosphere), data indicative of regulations associated with various locations (e.g., drinking water regulations, irrigation water regulations, soil regulations), and/or other data usable by the modeling compute devices 120 in simulating the capture of carbon from the atmosphere through enhanced rock weathering processes.\|[0035] In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. The system 100, in operation, provides innovative and independent geochemical models and modeling forecasts, filling a current gap in monitoring, reporting, and verification (MRV). Further, the system 100 contributes to the trust that is necessary for the scale-up of climate-tech carbon dioxide removal (CDR) industries to the gigaton level. While the system 100, in some embodiments, focuses on enhanced rock weathering, the science and technologies can also be applied to storing carbon dioxide in basalt and sandstone aquifers and mine tailings.\|[0036] A modeling forecast is useful at every stage of a project: conceptualization, contract negotiation, application, and post-project monitoring. The gateway 110, in the illustrative embodiment, is cloud-based, documented, and based on advanced cyberinfrastructure and data sciences that transform how modeling is delivered and how results are archived, analyzed, and presented. The gateway 110, in the illustrative embodiment, provides industry-standard authentication, authorization, and controlled sharing capabilities. Further, the system 100 provides provenance for the execution of tools, clonability, and reusability and integrates with national open cyberinfrastructure and public clouds for workflow execution.\|[0037] In the illustrative embodiment, the gateway 110 may serve four types of clients: a) technical specialists at stakeholders (CDR and purchaser corporations, regulatory agencies, environmental groups) who can search a large library of models 130 to find the likely outcomes for their projects; b) geochemical experts who can develop or tweak their models 130 on the gateway 110, but aided by automatic documentation, archives, and traceability on the gateway; c) stakeholders with no in-house capabilities who wish to outsource the initial development of models 130 and run the models 130 on the gateway 110; d) stakeholders who need independent models as certification. The availability of the gateway 110 may operate to broaden the participation of underrepresented groups and less developed countries, helping achieve the common goal of implementing scalable solutions around the world.\|[0038] Enhanced rock weathering can be generally represented with the equations shown below:\|[0039] Other equations representative of geochemical reactions are set forth in “Environmental Applications of Geochemical Modeling” by Chen Zhu and Greg Anderson, published in 2002, the contents of which are incorporated herein by reference. As discussed herein, characteristics of the soil and basalt in the soil can significantly impact the amount of carbon dioxide that will be captured and the amounts of metals (e.g., toxic metals) that may be introduced into the soil and water through the enhanced rock wreathing process. The models 130, in the illustrative embodiment, account for the characteristics through parameters discussed herein. Further, the models 130 incorporate features that are not present in conventional modeling systems, including the following: a. Near-equilibrium rates (e.g., in systems with relatively low Gibbs energy) are modeled to be one to two orders of magnitude slower than the far-from-equilibrium rates (e.g., in systems with relatively high Gibbs energy), rather than the far-from-equilibrium rate constants used in other models; b. basalt weathering is simulated as irreversible reactions with unidirectional rates (not reversible reactions in other models, which are theoretically wrong); and c. the models 130 include co-precipitation of toxic metals released from enhanced rock weathering with iron oxyhydroxides. Without co-precipitation in the models 130, the forecasts of toxic metal released into soil may incorrectly indicate toxic metal amounts in excess of applicable regulations. The models 130 may be fine-tuned with time, and more components may be added to the model 130.\|[0040] Further, the system 100, in the illustrative embodiment, provides a web-based model interface. Geochemical models are generally inaccessible to non-experts and the number of experts in the world is in short supply. The system 100 leverages expertise and experience of experts and makes modeling and modeling results available to non-experts. The gateway 110, in the illustrative embodiment, utilizes a database (e.g., the database 132) of mineralogical compositions of basalt feed stocks to be applied to croplands, and provides a web tool (e.g., a web based user interface) that allows users to input mineralogical compositions of the specific feed stock. Behind the web interface, the gateway 110 utilizes a database (e.g., the database 132) of different specific surface areas for different minerals. In operation, the gateway 110 may perform automatic input file generation (e.g., reformatting of parameter data into a format usable by the models 130).\|[0041] The web interface and models enable users (e.g., operating the target compute devices 150, 152, 154) to combine different parameters and run different scenarios to view resulting predictions of carbon capture through enhanced rock weathering and side effects thereof. For example, users may compare how much carbon dioxide is captured by applying 100 tons of basalt per hectare versus ten tons of basalt per hectare, and using one feed stock of basalt (e.g., Oregon basalt) versus another feed stock of basalt (e.g., Columbia River basalt). Users may also view the differences in carbon capture given different particle sizes. Further, users may view data that is indicative of toxic metal release into water and soil under varying conditions.\|[0042] In the illustrative embodiment, the gateway 110 may maintain a library of millions of simulations with a wide range of field conditions. The library may be searchable and the gateway 110 may enable users to locate modeling results and graphic presentations that fit their field conditions within minutes, rather than waiting for hours or longer for simulation results. The library may serve as a base for development or improvement of machine learning algorithms to (1) accelerate the simulations; and (2) find patterns, which lead to faster, more accurate, and more interpretable models. The models 130, in the illustrate embodiment, are calibrated geochemical models that bridge the gap between laboratory and field-based estimates of geochemical reactions. In particular, the models 130 may be calibrated with enhanced rock weathering batch scale laboratory experimental data, field data, and lysimeter experimental data. The results 134 may be embodied as databases and input files with adjusted parameters or semi-empirical scaling factors. In effect, the gateway 110 may provide independent, rigorous, models and modeling results that come with trust and creditability.\|[0043] While a relatively small number of compute devices 120, 140, 142, 144, 150, 152, 154 are shown in FIG. 1 for simplicity and clarity, it should be understood that the number of compute devices, in practice, may range in the tens, hundreds, thousands, or more. Likewise, it should be understood that the compute devices 120, 140, 142, 144, 150, 152, 154 may be distributed differently or perform different roles than the configuration shown in FIG. 1. Further, though shown as separate compute devices 120, 140, 142, 144, 150, 152, 154 in some embodiments, the functionality of one or more of the compute devices 120, 140, 142, 144, 150, 152, 154 may be combined into fewer compute devices and/or distributed across more compute devices than those shown in FIG. 1.\|[0044] Referring now to FIG. 2, an illustrative embodiment of a modeling compute device 120 includes a compute engine 210, an input/output (I/O) subsystem 216, communication circuitry 218, and one or more data storage devices 222. In some embodiments, the modeling compute device 120 may include one or more display devices 224 and/or one or more peripheral devices 226 (e.g., a mouse, a physical keyboard, etc.). In some embodiments, one or more of the illustrative components may be incorporated in, or otherwise form a portion of, another component. The compute engine 210 may be embodied as any type of device or collection of devices capable of performing various compute functions described below. In some embodiments, the compute engine 210 may be embodied as a single device such as an integrated circuit, an embedded system, a field-programmable gate array (FPGA), a system-on-a-chip (SOC), or other integrated system or device. Additionally, in the illustrative embodiment, the compute engine 210 includes or is embodied as a processor 212 and a memory 214. The processor 212 may be embodied as any type of processor capable of performing the functions described herein. For example, the processor 212 may be embodied as a single or multi-core processor(s), a microcontroller, or other processor or processing/controlling circuit. In some embodiments, the processor 212 may be embodied as, include, or be coupled to an FPGA, an application specific integrated circuit (ASIC), reconfigurable hardware or hardware circuitry, or other specialized hardware to facilitate performance of the functions described herein.\|[0045] In embodiments, the processor 212 is capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, a set of instructions which when executed by the processor 212 cause the modeling compute device 120 to perform one or more operations described herein. In embodiments, the processor 212 is further capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, one or more signals from external sources, e.g., from the peripheral devices 226 or via the communication circuitry 218 from an external compute device, external source, or external network. As one will appreciate, a signal may contain encoded instructions and/or information. In embodiments, once received, such a signal may first be stored, e.g., in the memory 214 or in the data storage device(s) 222, thereby allowing for a time delay in the receipt by the processor 212 before the processor 212 operates on a received signal. Likewise, the processor 212 may generate one or more output signals, which may be transmitted to an external device, e.g., an external memory or an external compute engine via the communication circuitry 218 or, e.g., to one or more display devices 224. In some embodiments, a signal may be subjected to a time shift in order to delay the signal. For example, a signal may be stored on one or more storage devices 222 to allow for a time shift prior to transmitting the signal to an external device. One will appreciate that the form of a particular signal will be determined by the particular encoding a signal is subject to at any point in its transmission (e.g., a signal stored will have a different encoding than a signal in transit, or, e.g., an analog signal will differ in form from a digital version of the signal prior to an analog-to-digital (A/D) conversion).\|[0046] The main memory 214 may be embodied as any type of volatile (e.g., dynamic random access memory (DRAM), etc.) or non-volatile memory or data storage capable of performing the functions described herein. Volatile memory may be a storage medium that requires power to maintain the state of data stored by the medium. In some embodiments, all or a portion of the main memory 214 may be integrated into the processor 212. In operation, the main memory 214 may store various software and data used during operation such as models, databases, simulation results, applications, libraries, and drivers.\|[0047] The compute engine 210 is communicatively coupled to other components of the modeling compute device 120 via the I/O subsystem 216, which may be embodied as circuitry and/or components to facilitate input/output operations with the compute engine 210 (e.g., with the processor 212 and the main memory 214) and other components of the modeling compute device 120. For example, the I/O subsystem 216 may be embodied as, or otherwise include, memory controller hubs, input/output control hubs, integrated sensor hubs, firmware devices, communication links (e.g., point-to-point links, bus links, wires, cables, light guides, printed circuit board traces, etc.), and/or other components and subsystems to facilitate the input/output operations. In some embodiments, the I/O subsystem 216 may form a portion of a system-on-a-chip (SoC) and be incorporated, along with one or more of the processor 212, the main memory 214, and other components of the modeling compute device 120, into the compute engine 210.\|[0048] The communication circuitry 218 may be embodied as any communication circuit, device, or collection thereof, capable of enabling communications over a network between the modeling compute device 120 and another device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). The communication circuitry 218 may be configured to use any one or more communication technology (e.g., wired or wireless communications) and associated protocols (e.g., Ethernet, Wi-Fi®, WiMAX, Bluetooth®, etc.) to effect such communication.\|[0049] The illustrative communication circuitry 218 includes a network interface controller (NIC) 220. The NIC 220 may be embodied as one or more add-in-boards, daughter cards, network interface cards, controller chips, chipsets, or other devices that may be used by the modeling compute device 120 to connect with another compute device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). In some embodiments, the NIC 220 may be embodied as part of a system-on-a-chip (SoC) that includes one or more processors, or included on a multichip package that also contains one or more processors. In some embodiments, the NIC 220 may include a local processor (not shown) and/or a local memory (not shown) that are both local to the NIC 220. Additionally or alternatively, in such embodiments, the local memory of the NIC 220 may be integrated into one or more components of the modeling compute device 120 at the board level, socket level, chip level, and/or other levels.\|[0050] Each data storage device 222, may be embodied as any type of device configured for short-term or long-term storage of data such as, for example, memory devices and circuits, memory cards, hard disk drives, solid-state drives, or other data storage device. Each data storage device 222 may include a system partition that stores data and firmware code for the data storage device 222 and one or more operating system partitions that store data files and executables for operating systems.\|[0051] Each display device 224 may be embodied as any device or circuitry (e.g., a liquid crystal display (LCD), a light emitting diode (LED) display, a cathode ray tube (CRT) display, etc.) configured to display visual information (e.g., text, graphics, etc.) to a user. In some embodiments, a display device 224 may be embodied as a touch screen (e.g., a screen incorporating resistive touchscreen sensors, capacitive touchscreen sensors, surface acoustic wave (SAW) touchscreen sensors, infrared touchscreen sensors, optical imaging touchscreen sensors, acoustic touchscreen sensors, and/or other type of touchscreen sensors) to detect selections of on-screen user interface elements or gestures from a user.\|[0052] In the illustrative embodiment, the components of the modeling compute device 120 are housed in a single unit. However, in other embodiments, the components may be in separate housings, in separate racks of a data center, and/or spread across multiple data centers or other facilities. The compute devices 140, 142, 144, 150, 152, 154 may have components similar to those described in FIG. 2 with reference to the modeling compute device 120. The description of those components of the modeling compute device 120 is equally applicable to the description of components of the compute devices 140, 142, 144, 150, 152, 154. Further, it should be appreciated that any of the devices 120, 140, 142, 144, 150, 152, 154 may include other components, sub-components, and devices commonly found in a computing device, which are not discussed above in reference to the modeling compute device 120 and not discussed herein for clarity of the description.\|[0053] In the illustrative embodiment, the compute devices 120, 140, 142, 144, 150, 152, 154 are in communication via a network 160, which may be embodied as any type of wired or wireless communication network, including global networks (e.g., the internet), wide area networks (WANs), local area networks (LANs), digital subscriber line (DSL) networks, cable networks (e.g., coaxial networks, fiber networks, etc.), cellular networks (e.g., Global System for Mobile Communications (GSM), Long Term Evolution (LTE), Worldwide Interoperability for Microwave Access (WiMAX), 3G, 4G, 5G, etc.), a radio area network (RAN), or any combination thereof.\|[0054] Referring now to FIG. 3, the system 100 (e.g., a modeling compute device 120 of the gateway 110) may perform a method 300 for modeling carbon dioxide removal through enhanced rock weathering. The method 300, in the illustrative embodiment, begins with block 302 in which the modeling compute device 120 obtains parameter data indicative of parameters for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering (e.g., the application of basalt dust to soil to increase the amount of carbon dioxide captured through the interaction of water (e.g., rain), carbon dioxide, and rock (e.g., the basalt dust)). In doing so, and as indicated in block 304, the modeling compute device 120 obtains data indicative of properties of soil in a location where the carbon dioxide is to be captured (e.g., removed from the atmosphere through enhanced rock weathering). In the illustrative embodiment, the modeling compute device 120 may obtain data indicative of minerals in the soil (e.g., a numeric value, such as a number indicative of a percentage of the soil comprising minerals), as indicated in block 306. As indicated in block 308, the modeling compute device 120 may obtain data indicative of carbon in the soil (e.g., a numeric value indicative of a percentage of the soil comprising carbon).\|[0055] The modeling compute device 120 may additionally obtain data indicative of effective porosity of the soil where the carbon is to be captured, as indicated in block 310. The effective porosity may be expressed, in at least some embodiments, as a numeric value (e.g., a percentage). As indicated in block 312, the modeling compute device 120 may obtain parameter data indicative of total specific surface area. In at least some embodiments, the total specific surface area may be expressed as square meters per gram. The modeling compute device 120 may obtain data indicative of the height of a top soil layer, as indicated in block 314. The height, in the illustrative embodiment, is expressed in meters. Further, the modeling compute device 120 may obtain data indicative of an amount of basalt added to the soil (e.g., tons per hectare), as indicated in block 316. Further, the modeling compute device 120 may obtain data indicative of basalt density, such as in grams per cubic centimeter, as indicated in block 318. Additionally, the modeling compute device 120 may obtain data indicative of bulk soil density, as indicated in block 320. The bulk soil density, in at least some embodiments, may be expressed as grams per cubic centimeter. The modeling compute device 120 may also obtain data indicative of basalt mineral composition, as indicated in block 322. The mineral composition of the basalt may be structured as one or more pairs of values, with each pair including an identifier (e.g., name, abbreviation, etc.) of a mineral and a corresponding percentage (e.g., indicative of a percentage of the basalt feed stock that the mineral constitutes).\|[0056] Still referring to FIG. 3, the modeling compute device 120 may obtain the parameter data as a function of (e.g., based on) an identification of the location where the carbon dioxide is to be captured in the soil, as indicated in block 324. In doing so, the modeling compute device 120 may read parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of properties of soil associated with location identifiers (e.g., plot numbers, geographic coordinates, zip codes, etc.), as indicated in block 326. In some embodiments, the modeling compute device 120 may obtain parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of mineral compositions from each of multiple basalt feed stocks, as indicated in block 328. Additionally or alternatively, the modeling compute device 120 may obtain parameter data through user input into corresponding fields (e.g., text boxes, check boxes, etc.) of a user interface (e.g., a graphical user interface presented by a target compute device 150, 152, 154 based on code (e.g., hypertext markup language (HTML) and/or JavaScript) and images (e.g., portable network graphics (PNG) files, Joint Photographic Experts Group (JPEG) files, or the like) transmitted from the modeling compute device 120 to the target compute device(s) 150, 152, 154 via the network 160, as indicated in block 330. An embodiment of a user interface 800 with which the modeling compute device 120 may obtain parameter data is shown in FIG. 8. The user interface 800 includes a first screen 810 that comprises parameter data about soil properties and a second screen 820 that includes parameter data about basalt mineral makeup. The user interface 800 provides one embodiment that users can use to input parameters related to soil properties and basalt mineral composition, run the models, and calculate how much CO2 can be sequestered.\|[0057] Referring now to FIG. 4, the method 300 continues in block 332 in which the modeling compute device 120 may calculate, as a function of the obtained parameter data, additional parameter data for use by one or more models (e.g., the models 130). In doing so, the modeling compute device 120 may calculate air and blind pores (e.g., a numeric value), as indicated in block 334. The modeling compute device 120 may additionally calculate a volume of soil per hectare, as indicated in block 336. Further, the modeling compute device 120 may calculate a number of volume (e.g., liters) of pore water per unit of area (e.g., hectare), as indicated in block 338. Additionally, the modeling compute device 120 may calculate a mass of basalt per unit of volume of the soil, as indicated in block 340. In addition, the modeling compute device 120 may calculate a concentration of basalt in the soil, as indicated in block 342. Further, the modeling compute device 120 may calculate a total weight percentage, as indicated in block 344. The modeling compute device 120 may also calculate a rock specific surface area, as indicated in block 346. In addition, the modeling compute device 120 may calculate a total surface area, in block 348. In performing the calculations, the modeling compute device 120 may utilize a database (e.g., a database 132) of specific surface areas for each of a set of minerals (e.g., minerals in the soil, in the basalt, etc.), as indicated in block 350. An embodiment of a user interface 900 in which the modeling compute device 120 may display additional parameters calculated as discussed above is shown in FIG. 9. In some embodiments, the user interface 800 includes a third screen 830 that may display additional parameters calculated as discussed above.\|[0058] After obtaining the parameter data, the method 300, in the illustrative embodiment, advances to block 352, in which the modeling compute device 120 produces, using one or models from a library of models (e.g., the models 130), one or more predictions indicative of an amount of carbon dioxide that will be removed from the atmosphere (e.g., captured through enhanced rock weathering). In doing so, the modeling compute device 120 may select one or more models 130 as a function of the obtained parameter data, as indicated in block 354. That is, the modeling compute device 120 may select one or more models 130 from the library of models as a function of a determined similarity (e.g., a similarity score, such as a calculated distance (e.g., a Euclidean distance, a cosine similarity, a result of a clustering analysis, etc.)) of the parameter data (e.g., obtained in block 302) to reference parameters for which one or more corresponding models 130 have been identified (e.g., in a data set in the memory 214 or storage 222, in a database 132, etc.) as having a high accuracy of predictions (e.g., the results 134 produced by those models have been shown to predict within a predefined threshold of accuracy (e.g., a defined percentage), actual results that were later measured in field tests). That is, if a particular model 130 is identified as more accurately predicting the amount of carbon dioxide that will be removed from the atmosphere than other models, when the parameters are similar to those obtained in block 302, the modeling compute device 120 may select that model for use.\|[0059] In some embodiments, as indicated in block 358, the modeling compute device 120 may select one or more models 130 as a function of a distance of the location where the carbon dioxide is to be captured to each of a set of reference locations associated with the models 130. That is, a data set (e.g., in the memory 214, the data storage 222, or a database 132) may identify a location (e.g., a zip code, a set of geographic coordinates, or other identifier of a location) with each model 130 in the library (e.g., because the corresponding model 130 has been shown to produce predictions with high accuracy for the associated location) and the modeling compute device 120 may select a set (e.g., one or more) of the models 130 that are closest to the location where the carbon dioxide is to be captured.\|[0060] Referring now to FIG. 5, in block 360, the modeling compute device 120 may reformat the parameter data for use by the models 130 (e.g., by converting the data into a file format that the models 130 are configured to parse (e.g., using a scripting language such as Python)). As indicated in block 362, the modeling compute device 120 may select one or more machine learning models (e.g., models, such as neural networks, decision trees, or others that may iteratively improve in prediction accuracy based on feedback). In some embodiments, the modeling compute device 120 may select an ensemble (e.g., a combination of models, in which outputs of the individual models may be weighted relative to each other), as indicated in block 364. The models 130 may include one or more models implemented by PHREEQC (e.g., PHREEQC 3), from the U.S. Geological Survey, GEM (e.g., reservoir modeling), TOUGHREACT from Lawrence Berkeley National Laboratory, and/or other models (e.g., provided by entities associated with one or more of the source compute devices 140, 142, 144). The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period, as indicated in block 366. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured each year of a defined number of years at the specified location, as indicated in block 368.\|[0061] The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per unit of area, as indicated in block 370. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per hectare, as indicated in block 372. In the illustrative embodiment, and unlike conventional systems, the modeling compute device 120 utilizes models that simulate co-precipitation of iron with toxic metals, as indicated in block 374. Additionally, and unlike conventional systems, the modeling compute device 120, in the illustrative embodiment, utilizes models that simulate basalt weathering as irreversible reactions with unidirectional rates, as indicated in block 376. Further, and unlike conventional systems, the modeling compute device 120 in the illustrative embodiment utilizes models in which near-equilibrium (e.g., within a defined percentage of an equilibrium state) rates are one to two orders of magnitude slower than far-from-equilibrium (e.g., not within the defined percentage of the equilibrium state) rates, as indicated in block 378. Further, and as indicated in block 380, the modeling compute device 120, in the illustrative embodiment, produces one or more predictions indicative of toxic metal concentrations in water associated with the location where the carbon dioxide is to be captured. In doing so, the modeling compute device 120 may produce one or more predictions indicative of concentrations of Nickel, Chromium, and/or Cadmium in the water, as indicated in block 382.\|[0062] Referring now to FIG. 6, the modeling compute device 120 may produce the one or more predications as a function of depth (e.g., depth of the water), as indicated in block 384. As indicated in block 386, the modeling compute device 120 may produce the one or more predictions regarding toxic metals in the water as a function of time (e.g., amount of toxic metals in the water per year). In some embodiments, the modeling compute device 120 may produce the predictions of toxic metals in the water relative to one or more regulations associated with the location where the carbon dioxide is to be captured, as indicated in block 388. That is, the modeling compute device 120 may obtain data (e.g., from a database 132, from a source compute device 140, 142, 144) indicative of applicable regulations and indicate whether the predicted amount of toxic metals satisfies (e.g., does not violate the regulation(s), is close to (e.g., within a defined percentage of), etc.) a limit specified by the regulations. The modeling compute device 120 may produce the prediction(s) relative to drinking water regulations and/or irrigation water regulations, as indicated in blocks 390, 392. The modeling compute device 120 may produce one or more predictions indicative of toxic metal concentrations in the soil associated with the location where the carbon dioxide is to be captured, as indicated in block 394. In doing so, the modeling compute device 120 may produce prediction(s) indicative of concentrations of Nickel, Chromium, and/or Cadmium in the soil, as indicated in block 396. The modeling compute device 120 may produce the prediction(s) as a function of depth (e.g., in the soil) and/or as a function of time, as indicated in blocks 398, 400. Similar to block 388, the modeling compute device 120 may produce the prediction(s) of toxic metals in the soil relative to one or more regulations associated with the location, as indicated in block 402.\|[0063] Referring now to FIG. 7, the modeling compute device 120 may produce data indicative of probabilities (e.g., confidence) associated with the one or more predictions, as indicated in block 404. For example, the modeling compute device 120 may produce a predictions as confidence intervals, with one prediction associated with a particular level of confidence (e.g., a percentage of likelihood), and one or more other predictions associated with other levels of confidence. As indicated in block 406, the modeling compute device 120 may determine an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. For example, the modeling compute device 120 may obtain data (e.g., from a source compute device 140, 142, 144, a database 132, etc.) indicative of a conversion rate between tons of carbon captured and a number of corresponding carbon credits and multiply the predicted amount of carbon dioxide by the conversion rate to determine the amount of carbon credits. In some embodiments, the modeling compute device 120 may adjust the number of carbon credits based on a probability or confidence level associated with the predicted amount of carbon dioxide to be removed from block 404 (e.g., by multiplying the amount of carbon dioxide by a percentage associated with the probability or confidence level). As indicated in block 408, the modeling compute device 120 may determine soil parameters that will increase capture of carbon dioxide at the location. For example, and as indicated in block 410, the modeling compute device 120 may determine, from a set of multiple basalt feed stocks, each having different mineral compositions and/or other properties, a basalt feed stock predicted to capture the most carbon dioxide in the location while maintaining compliance with regulations (e.g., toxic metals in the soil, toxic metals in the water). The modeling compute device 120 may do so by simulating carbon dioxide capture with each of the basalt feed stocks using the models 130 and identifying the basalt feed stock that satisfies the above conditions to the greatest degree.\|[0064] Continuing the method 300, the modeling compute device 120 may present a visual representation of the one or more prediction(s) in a user interface, as indicated in block 412. In the illustrative embodiment, the modeling compute device 120 produces visual presentation(s) of the prediction(s) in a web based interface (e.g., based on a HTML, JavaScript, and image data sent from the modeling compute device 120 to one or more rending engines (e.g., web browser(s)) executed by corresponding target compute devices 150, 152, 154). As indicated in block 416, in producing one or more visual representations of the prediction(s), the modeling compute device 120 may present visual representations that include interactive graphs (e.g., in which time periods, depths, or other parameters may be selected and a corresponding graph is presented). Example embodiments of visual representations 1000, 1100, 1200, 1300, 1400 of the predictions that may be presented by the modeling compute device 120 and displayed by one or more of the corresponding target compute devices 150, 152, 154 are shown in FIGS. 10-14.\|[0065] While certain illustrative embodiments have been described in detail in the drawings and the foregoing description, such an illustration and description is to be considered as exemplary and not restrictive in character, it being understood that only illustrative embodiments have been shown and described and that all changes and modifications that come within the spirit of the disclosure are desired to be protected. There exists a plurality of advantages of the present disclosure arising from the various features of the apparatus, systems, and methods described herein. It will be noted that alternative embodiments of the apparatus, systems, and methods of the present disclosure may not include all of the features described, yet still benefit from at least some of the advantages of such features. Those of ordinary skill in the art may readily devise their own implementations of the apparatus, systems, and methods that incorporate one or more of the features of the present disclosure.	Family Number\|(117356463)\|117356463\|Object of Invention\|(US20260017435 A1)\| (...) the following features which, alone or in any combination, may comprise patentable subject matter:According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering.\|In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. \|Abstract\|(US20260017435 A1)\|Technologies for modeling carbon dioxide removal include a compute device with circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may also be configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Further, the circuitry may be configured to present a visual representation of the at least one prediction in a user interface. Other embodiments are also described and claimed.\|Title\|(US20260017435 A1)\|Technologies for modeling carbon dioxide removal\|Advantages / Prev. Drawbacks\|(US20260017435 A1)\|Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.\|Independent Claims\|(US20260017435 A1)\| (...) obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| (...) obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| (...) obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\|	Computer technology\|Environmental technology	B01D-053/62\|B01D-053/82\|B01D-2257/504\|G06F-030/27		B01D-053/62\|B01D-053/82\|B01D-2257/504\|G06F-030/27	B01D-053/62\|B01D-053/82\|G06F-030/27	B01D-053/62\|B01D-053/82\|G06F-030/27										PENDING	(US20260017435)\|PENDING	ALIVE	(US20260017435)\|ALIVE	(US20260017435)\|LEGAL DETAILS FOR US20260017435\|Actual or expected expiration date=2045-07-09\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-07-09\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19264502\|Application date=2025-07-09\|Standardized application number=2025US-19264502\|Event publication date=2025-07-09\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-07-09\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-07-09\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 29920-426689\|Event publication date=2025-07-09\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 138060\|Event publication date=2025-07-09\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2025-07-09\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-07-09\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-07-25\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2025-07-29\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-09-29\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-10-02\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2025-10-22\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-10-22\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2026-01-15\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20260017435\|Publication stage code=A1\|Publication date=2026-01-15\|Standardized publication number=US20260017435\|Event publication date=2026-01-16\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification		(US20260017435)\|US	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcP7LGmymc8G11q5LJ03xVJIJjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023247689&ekey=1952&xpn=US20260017435&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19264502/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=rCUZBbi%252Bv%252B%252FyiDX9GDUoPcRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(US20260017435)\|US	(US20260017435)\|NAME=THE TRUSTEES OF INDIANA UNIVERSITY , CITY=Bloomington , STATE=IN , COUNTRY=US			(US20260017435)\|US	(US20260017435)\|NAME=Zhu Chen, CITY=Bloomington, STATE=IN , COUNTRY=US	(US20260017435)\|14	2	1					(US20260017435)\|Number of Claims: NCL=20\|Number of Drawings: NDR=14\|Number of Figures: NFG=14\|Independent Claim Number: ICL=1,14,19\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|	(US20260017435)\|Provisional Appl: US63/669,351 FDD=2024-07-10 [2024US-63669351]	(US20260017435)\|ENGLISH (ENG)	(US20260017435)\|Patent	Titre: (US20260017435)\|Technologies for modeling carbon dioxide removal Résumé: (US20260017435)\|Technologies for modeling carbon dioxide removal include a compute device with circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may also be configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Further, the circuitry may be configured to present a visual representation of the at least one prediction in a user interface. Other embodiments are also described and claimed.	1	Abstract	gpt-4o-mini	yes	The article discusses enhanced rock weathering as a method for carbon dioxide removal, which aligns with the topic of accelerated weathering of rocks for CO₂ capture.
4	US63/601,059P\|US18/954,208	US18/954,208	US20250164404	114579754	US20250164404 A1 2025-05-22 [US20250164404]	2023-11-20\|2024-11-20	2024-11-20	2025-05-22		(US20250164404)\|2044-11-20	(US20250164404)\|System and method for enhanced rock weathering monitoring, reporting, and verification	(US20250164404)\|A method and system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. In some embodiments, the method includes emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area. The method includes determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target. The method includes converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target. The method also includes analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools. The method further includes providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.	IMPOSSIBLE SENSING\|MATI CARBON PBC	(US20250164404)\|Impossible Sensing LLC ([US])\|Mati Carbon PBC ([US])	SOBRON PABLO\|JORDAN JACOB S\|AGARWAL SHANTANU	(US20250164404)\|Sobron Pablo\|Jordan Jacob S.\|Agarwal Shantanu		(US20250164404)\|By measuring the SOC level, the present disclosure facilitates the correlation between changes in organic carbon attributable to rock dust application, thereby offering valuable insights into soil improvement.\|The present system allows improved statistical accuracy with pooled/composite soil samples, as shown in 402.\|This dual system enables the simultaneous determination of organic carbon and elemental composition in samples. This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status.\|However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions.\|However, understanding the ecosystematic changes in soils is complex, as conditions may vary across a single plot of land.\|MRV is technically difficult due to the long timescales and uncertainties associated with the chemical and physical processes involved.\|	(US20250164404)\|1. A system for monitoring, reporting, and verification of enhanced rock weathering comprising: a spectroscopy device comprising an optical source and a detector, wherein the optical source is configured to emit one or more optical signals directed to a target collected from a target area, and the detector is configured to determine spectral measurements of the optical signals collected from the target; and a data analysis subsystem coupled to the spectroscopy device and configured to: convert the spectral measurements to data indicating compositional characteristics of the target; analyze the data indicating compositional characteristics of the target using a plurality of analytical tools; and provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\|14. A method for monitoring, reporting, and verification of enhanced rock weathering comprising: emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area; determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target; and converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target; analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools; and providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.\|	(US20250164404)\|In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for calculating heavy metal concentrations 308, e.g., the amounts of metallic elements (often toxic) found in the soils or rock dust used for ERW.\|In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating specific soil elements 306, for example, the nitrogen (N), phosphorus (P), and potassium (K) content of the soil.\|In some embodiments, the present disclosure describes a LIBS device (e.g., 204) used for determining weathering status 304.\|	(US20250164404)\|ENHANCED ROCK(100,22)\|REPORTING(100,13)\|MONITORING(100,11)\|VERIFICATION(100,7)\|ENHANCED ROCK VERIFICATION(100,4)\|SPECTRAL MEASUREMENT(90,13)\|SPECTROSCOPY(69,19)\|ANALYTICAL INSTRUMENT(59,9)\|WEATHERING STATUS(56,9)\|DRY LAND EVALUATION(55,1)\|ENHANCED ROCK WEATHERING VERIFICATION(51,2)\|SOIL COMPLEXITY(51,1)\|ASSESSMENT(48,10)\|DATA ANALYSIS SUBSYSTEM(47,25)\|WEATHERING PREDICTION(45,6)\|INSIGHT(41,13)\|IDENTIFYING GEOLOCATED ZONE(41,1)\|STATISTICAL ACCURACY(40,1)\|EMPIRICAL MODEL(38,7)\|MULTIVARIATE DISTRIBUTION MODEL(36,6)\|VALUABLE INSIGHT(36,3)\|POOLED SAMPLE(33,12)\|ECOSYSTEMATIC CHANGE(32,1)\|HEAVY CATION(29,2)\|CATION COVARIANCE ANALYSIS(28,6)\|ROCK LOSS(27,3)\|SIGNAL TRANSMITTER(26,2)\|LONG TIMESCALE(26,1)\|EARTH AUGER(25,5)\|CARBON CREDIT CREATION(24,6)\|ENHANCED WEATHERING POTENTIAL(23,7)\|CARBON DIOXIDE REMOVAL(22,31)\|LAND SINGLE PLOT(22,1)\|UNCERTAINTY(21,2)\|DATA ANALYSIS(20,29)\|SOILS(20,8)\|CARBON DIOXIDE(19,36)\|CORRELATION(19,2)\|LIGHT CATION(19,2)\|LASER INDUCED BREAKDOWN SPECTROSCOPY(18,132)\|ENHANCED ROCK WEATHERING(17,41)\|TARGET AREA(16,26)\|ORGANIC CARBON(16,3)\|SOIL IMPROVEMENT(16,1)\|BIOAVAILABLE NUTRIENT QUANTIFICATION(15,1)\|SINGLE PLOT(15,1)\|MRV(14,16)\|CALCULATING HEAVY METAL(14,2)\|PATCHWORK SMALLHOLDER FARM(14,1)\|SOIL SAMPLE(13,11)\|CALIBRATION CURVE(13,10)\|INFIELD DEPLOYMENT(13,3)\|COVARIANCE COMPREHENSIVE ASSESSMENT(13,1)\|INTERSAMPLE HETEROGENEITY COMPREHENSIVE EXAMINATION(13,1)\|PELLETIZED SUBSAMPLE RASTERED ANALYSIS(13,1)\|HEAVY METAL(12,10)\|ROCK(11,5)\|IGNITION(11,3)\|SOIL HETEROGENEITY(11,3)\|COMPOSITIONAL CHARACTERIZATION(11,2)\|ECONOMICALLY DISADVANTAGED COMMUNITY(11,1)\|PHOSPHORUS P(11,1)\|OCEAN ACIDIFICATION(10,2)\|PREDICTION MODEL(10,2)\|INCENTIVIZE EMISSION AVOIDANCE(10,1)\|OCEAN FLORA HEALTH(10,1)\|ROBUST MRV FRAMEWORK(10,1)\|TOTAL CARBON DIOXIDE(9,6)\|AUTOFOCUSING COMPONENT(9,5)\|OPTICAL SOURCE(9,5)\|AGRICULTURAL SETTING(9,4)\|DEPTH INTEGRATED SOIL PROFILE(9,4)\|INDUCTIVELY COUPLED PLASMA(9,4)\|AQUEOUS METAL(9,3)\|CARBON CREDIT GENERATION CREDIBILITY(9,3)\|MANAGING STATE(9,3)\|GEOLOCATED ZONE SOIL SAMPLING(9,1)\|GRADUAL ROCK DISSOLUTION(9,1)\|ROCK WEATHERING STATUS(9,1)\|CARBON CAPTURE(8,8)\|ORGANIC CARBON MEASUREMENT(8,3)\|AGRONOMIC COBENEFIT(8,1)\|BASALT DISSOLUTION(8,1)\|CORAL ECOSYSTEM(8,1)\|DISHONEST ACTOR(8,1)\|DOMINANT SPECIATION(8,1)\|ENHANCE OCEAN ALKALINITY(8,1)\|GEOLOCATED ZONE SAMPLING(8,1)\|GROUNDWATER RUNOFF(8,1)\|INVALUABLE INSIGHT(8,1)\|NUTRIENT REQUIREMENT ESTIMATION(8,1)\|PREDICTING WEATHERING(8,1)\|PULVERIZED ROCK DUST(8,1)\|ROCK MINERAL BREAKDOWN(8,1)\|SOIL PENETRATION(8,1)\|TRADABLE CERTIFICATE(8,1)\|ALKALI SILICATE MINERAL(7,3)\|EMPIRICALLY DRIVEN MODEL(7,3)\|LIGHT COLLECTION OPTICS(7,3)\|AGRICULTURAL LAND(7,2)\|GRAPHICAL REPRESENTATION(7,2)\|AGRICULTURAL SOILS(7,1)\|BICARBONATE PRECIPITATION(7,1)\|BROAD ELEMENTAL COVERAGE(7,1)\|CENTRAL COMPOSITIONAL TENDENCY ASSESSMENT(7,1)\|COLLABORATIVE FRAMEWORK(7,1)\|FLUORESCENCE SPECTRUM(7,1)\|FORESTRY INTERVENTION(7,1)\|GEOLOGICAL ATTRIBUTE(7,1)\|ICP MS CALIBRATION INTEGRATION(7,1)\|RELIABLE CALIBRATION FRAMEWORK(7,1)\|ROBUST CALIBRATION(7,1)\|ROOT RESPIRATION(7,1)\|SOIL SUITABILITY(7,1)\|SPATIAL HETEROGENEITY GRANULAR UNDERSTANDING(7,1)\|STANDARDIZED REPORTING(7,1)\|SYSTEMATIC VARIABILITY(7,1)\|TANGIBLE NONVOLATILE PROGRAM CARRIER(7,1)\|UNLISTED ITEM(7,1)\|WEATHERING OUTCOME(7,1)\|ANALYSIS COMPONENT(6,8)\|GENERATING CARBON CREDIT(6,4)\|DEPTH INTERVAL(6,2)\|ELEMENTAL COMPOSITION ANALYSIS(6,2)\|KEY CATION(6,2)\|MOTOR INSTRUMENT(6,2)\|QUANTITATIVE ELEMENTAL ANALYSIS(6,2)\|RASTER PATTERN(6,2)\|SEED MATTER(6,2)\|SOIL COLUMN(6,2)\|SUBCOMBINATION(6,2)\|SUPPORTING DATA(6,2)\|ACIDIC SOIL REMEDIATION(6,1)\|ADDRESS CHALLENGING(6,1)\|AGRONOMIC BENEFIT(6,1)\|BUYER CONCERN(6,1)\|CARBON SEQUESTRATION KNOWABILITY(6,1)\|CRUCIAL INSIGHT(6,1)\|CRUCIAL ISSUE(6,1)\|DECISION INFORMATION(6,1)\|DEEP AQUIFER(6,1)\|DISSOLVE BICARBONATE(6,1)\|ELEMENTAL IDENTIFICATION(6,1)\|FARMER BURDEN(6,1)\|INTEGRATING UNCERTAINTY MODELING(6,1)\|MARKUP LANGUAGE(6,1)\|MEASUREMENT MISFIT(6,1)\|MINERAL CLASSIFICATION(6,1)\|MOBIL INSTRUMENT(6,1)\|MULTITHREADED PROCESSOR(6,1)\|PELLETIZING SOIL(6,1)\|POOLED SAMPLE UTILIZATION(6,1)\|PRESSED PELLETIZED SUBSAMPLE(6,1)\|REPLANT TREE(6,1)\|ROCK DUST ARRAY(6,1)\|SCRIPT INSTRUCTION(6,1)\|SOIL FERTILITY ASSESSMENT(6,1)\|SOIL SPATIAL VARIABILITY(6,1)\|SUBSURFACE NEAR CROP(6,1)\|UNTREATED SEWAGE SLUDGE(6,1)\|VERSATILE SAMPLING(6,1)\|SOIL ORGANIC CARBON(5,10)\|HCO(5,6)\|MRV(5,6)\|METAL(5,5)\|DECISION MAKING INFORMATION(5,3)\|FERTILIZER(5,3)\|MEASURING CARBON(5,3)\|SEA(5,3)\|TARGET SAMPLE(5,3)\|SAMPLE PROBE(5,2)\|3G WIRELESS MODEM(5,1)\|4G WIRELESS MODEM(5,1)\|ABSENT INCLUSION(5,1)\|ALKALINE MINERAL(5,1)\|ANALYTICAL ACCURACY(5,1)\|BASALT WEATHERING REACTION(5,1)\|BICARBONATE DRAW(5,1)\|COMPOSITIONAL ANALYSIS(5,1)\|COORDINATED FILE(5,1)\|COVARIANCE RELATIONSHIP(5,1)\|DEMAND FULFILLMENT(5,1)\|DEPTH PROFILING(5,1)\|DETECTING CARBON DECEPTION(5,1)\|DISSOLVED CARBON DOMINANT(5,1)\|ECOLOGICAL RISK(5,1)\|EXCLUSIVITY TERM(5,1)\|FUTURE OBSTACLE(5,1)\|GRID ANALYSIS(5,1)\|INFIELD ANALYSIS(5,1)\|INSTRUCTION INTERPRETATION(5,1)\|LASER IRRADIATION(5,1)\|MINERAL BICARBONATE(5,1)\|MODELING UNCERTAINTY(5,1)\|MRV QUALITY(5,1)\|NONNORMAL DISTRIBUTION(5,1)\|PH AMENDMENT(5,1)\|PHYSICAL(5,1)\|PLASMA PLUME(5,1)\|POOLED SAMPLE ACCURATE MEASUREMENT(5,1)\|PRECISE CHARACTERIZATION(5,1)\|PROCESSOR FIRMWARE(5,1)\|QUANTIFICATION ANALYSIS(5,1)\|RAW ROCK SAMPLE(5,1)\|REPORT CARBON SEQUESTRATION(5,1)\|ROBUST ANALYSIS(5,1)\|ROBUST MONITORING(5,1)\|SAMPLE HANDING(5,1)\|SATELLITE SENSOR(5,1)\|SERVER DISTRIBUTION(5,1)\|SOIL QUALITY PRECISE ASSESSMENT(5,1)\|SOILS TRANSITION(5,1)\|SPECTROSCOPY MEASUREMENT(5,1)\|TARGET VARIANCE(5,1)\|VERIFIABLE CARBON CREDIT(5,1)\|WORKFLOW PROPOSITION(5,1)\|CARBON DISSOLUTION(4,2)\|CENTRALIZED COMPUTING(4,2)\|GRAVEL(4,2)\|MULTITASKING(4,2)\|OPTIMIZATION(4,2)\|TRACTOR(4,2)\|ADJUSTING ROCK(4,1)\|AGGREGATING SOIL SAMPLE(4,1)\|ALKALINE SILICATE MINERAL POTENTIAL(4,1)\|BASELINE INFORMATION(4,1)\|CALCIUM CARBONATE MINERAL(4,1)\|CALCULATION REPRESENTATION(4,1)\|CARBON BEHAVIOR(4,1)\|CARBON CREDIT GENERATION RELIABILITY(4,1)\|CARBON CREDIT SALE(4,1)\|CARBON DIOXIDE SEQUESTRATION POTENTIAL(4,1)\|CARBON MEASUREMENT ISSUE(4,1)\|CARBON STORAGE PERMANENCE(4,1)\|CARBON UPTAKE(4,1)\|CLOUD PROCESSING(4,1)\|CLOUD STORAGE(4,1)\|COMPUTING ENVIRONMENT(4,1)\|DEEP UNDERSTANDING(4,1)\|EMBODIED COMPUTER SOFTWARE(4,1)\|ENHANCING MEASURE(4,1)\|ENSURING STABILITY(4,1)\|EXECUTION ENVIRONMENT(4,1)\|FLASH MEMORY(4,1)\|FOSSIL FUEL COMPANY(4,1)\|GEOLOGICAL TIMESCALE(4,1)\|INITIATIVE(4,1)\|INORGANIC CARBON AQUEOUS SPECIES(4,1)\|INSTANTIATION(4,1)\|MAJOR AQUEOUS SPECIES(4,1)\|MICROHETEROGENEITY(4,1)\|MIDDLEWARE COMPONENT(4,1)\|MOBILE VEHICLE(4,1)\|NET EMISSION(4,1)\|ORDINAL TERM(4,1)\|ORDINARY MEANING(4,1)\|PH RISE(4,1)\|PHYTOREMEDIATION(4,1)\|POOLED SOIL SAMPLE(4,1)\|POOLING SAMPLE(4,1)\|PRIMARY FACET(4,1)\|QUANTIFYING CARBON CREDIT(4,1)\|QUICK ADJUSTMENT(4,1)\|ROBOTIC ARM(4,1)\|ROCK POWDER(4,1)\|SAMPLE PRESENTATION(4,1)\|SOIL QUALITY ASSESSMENT(4,1)\|SOIL SAMPLING TECHNIQUE ADVANCE(4,1)\|SPECIES DISTRIBUTION(4,1)\|STANDARDIZED SUBSTRATE(4,1)\|TRUSTWORTHINESS(4,1)\|VARIABLE FOCUS LENS(4,1)\|WIRELESS INTERFACE(4,1)\|MACHINE LEARNING(3,3)\|SOIL SAMPLE COLLECTION(3,3)\|STRATEGY(3,3)\|WEB BROWSER(3,3)\|STRUCTURED GRID(3,2)\|ACCOUNTABILITY(3,1)\|AGNOSTIC(3,1)\|AGRICULTURAL MACHINERY(3,1)\|ANALYSIS REPRESENTATION(3,1)\|APPLYING CRUSHED ROCK PRACTICE(3,1)\|ARTIFICIALLY GENERATED PROPAGATED SIGNAL(3,1)\|ATMOSPHERIC CARBON DIOXIDE(3,1)\|AUDITORY FEEDBACK(3,1)\|BASELINE DATA(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON GAIN(3,1)\|CENTURY(3,1)\|CHANGING GROUND(3,1)\|CLIENT SERVER RELATIONSHIP(3,1)\|COLLECTED LIGHT PULSE(3,1)\|COMPARABILITY(3,1)\|COMPOSITIONAL ARRAY RANGE(3,1)\|COMPUTER PROGRAM INSTRUCTION(3,1)\|CONSERVATION(3,1)\|CREATING CARBON CREDIT(3,1)\|DEDUCE(3,1)\|DISCRETE REGION(3,1)\|DISPLAYING INFORMATION(3,1)\|DRONE(3,1)\|DUST SAMPLE(3,1)\|EMISSION TEST(3,1)\|ENHANCED WEATHERING PRACTICE(3,1)\|ENVIRONMENTAL ASSESSMENT(3,1)\|EQUIVALENT STRUCTURE(3,1)\|EXPRESS SUPPORT(3,1)\|FACTORING(3,1)\|FITTING MULTIVARIATE NORMAL(3,1)\|GAME CONSOLE(3,1)\|	(US20250164404)\|What is claimed is:\|1. A system for monitoring, reporting, and verification of enhanced rock weathering comprising:\| a spectroscopy device comprising an optical source and a detector, wherein the optical source is configured to emit one or more optical signals directed to a target collected from a target area, and the detector is configured to determine spectral measurements of the optical signals collected from the target; and\| a data analysis subsystem coupled to the spectroscopy device and configured to:\| convert the spectral measurements to data indicating compositional characteristics of the target;\| analyze the data indicating compositional characteristics of the target using a plurality of analytical tools; and\| provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\|2. The system of claim 1, wherein, to convert the spectral measurements to the data indicating compositional characteristics of the target, the data analysis subsystem is further configured to determine a weathering status, evaluate target contents, calculate heavy metal concentration, determine metal ratios in the target, or measure organic carbon in the target.\|3. The system of claim 2, wherein, to determine the weathering status, the data analysis subsystem is further configured to determine loss of rock dust by assessing composition of cations in rock dust applied to the target area through the enhanced rock weathering.\|4. The system of claim 2, wherein the heavy metal concentration is calculated in response to receiving bio-availability of metals and dissolved aqueous metals.\|5. The system of claim 2, wherein the soil organic carbon is measured based on determining loss of material on ignition.\|6. The system of claim 1, wherein the target is a pooled sample that includes soil samples collected and combined from multiple locations within the target area.\|7. The system of claim 6, further comprising a sampling handing unit configured to identify geolocated zones within the target area from which the pooled sample is collected, wherein the pooled sample is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling.\|8. The system of claim 1, wherein, to analyze the data indicating compositional characteristics, the data analysis subsystem is further configured to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS.\|9. The system of claim 1, wherein, to provide the assessments on carbon dioxide removal and insights on enhanced rock weathering, the data analysis subsystem is further configured to create a prediction model to provide data support for subsequent implementation of enhanced rock weathering.\|10. The system of claim 1, wherein, to provide the assessments on carbon dioxide removal and insights on enhanced rock weathering, the data analysis subsystem is further configured to determine one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.\|11. The system of claim 1, wherein the spectroscopy device is a handheld LIBS device.\|12. The system of claim 1, wherein the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and wherein the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis.\|13. The system of claim 1, wherein the spectroscopy device is a LIBS device that is combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic from the target.\|14. A method for monitoring, reporting, and verification of enhanced rock weathering comprising:\| emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area;\| determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target; and\| converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target;\| analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools; and\| providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.\|15. The method of claim 14, wherein converting the spectral measurements comprises one or more of determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target.\|16. The method of claim 15, wherein determining the weathering status comprises determining loss of rock dust by assessing composition of cations in rock dust applied to the target area through the enhanced rock weathering.\|17. The method of claim 14, further comprising identifying geolocated zones within the target area from which the target is collected, wherein the target is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling.\|18. The method of claim 14, wherein analyzing the data indicating compositional characteristics comprises performing one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS.\|19. The method of claim 14, wherein providing the assessments on carbon dioxide removal and insights on enhanced rock weathering comprises determining one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.\|20. The method of claim 14, wherein the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and wherein the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis.	(US20250164404)\|CROSS REFERENCE TO RELATED APPLICATION\|[0001] This application claims the benefit of U.S. Provisional Patent Application No. 63/601,059, titled “System and Method for Enhanced Rock Weathering Monitoring, Reporting, and Verification,” and filed on Nov. 20, 2023, the entire content of which is incorporated by reference herein.\|(US20250164404)\|TECHNICAL FIELD\|[0002] This disclosure relates to compositional characterization techniques, in particular, to optical devices that embody new methodologies for monitoring, reporting, and verification (MRV) of enhanced rock weathering (ERW).\|BACKGROUND\|[0003] Enhanced rock weathering (ERW) is the practice of applying crushed rocks and silicate minerals to agricultural land. It is a promising scalable and cost-effective carbon dioxide removal (CDR) strategy with significant environmental and agronomic co-benefits. However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions. Most current projects/systems/devices cannot accurately obtain carbon measurement and properly report carbon sequestration. Also, ERW lacks a robust monitoring, reporting, and verification (MRV) framework to address challenging problems such as carbon deception. For example, current MRV practices cannot provide a framework to easily detect and process a fraudulent claim of carbon gains by dishonest actors in the system.\|SUMMARY\|[0004] To address the aforementioned shortcomings, a method and a system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. The method include using a spectroscopy device to emit one or more optical signals directed to a target collected from a target area and to determine spectral measurements of the optical signals collected from the target. The method also includes using a data analysis subsystem to convert the spectral measurements to data indicating compositional characteristics of the target, analyze the data indicating compositional characteristics of the target using a plurality of analytical tools, and provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\|[0005] To convert the spectral measurements to the data indicating compositional characteristics of the target, one or more of the processes, such as determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. To determine the weathering status, loss of rock dust is determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering. To analyze the data indicating compositional characteristics, analytical tools are used to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS. To provide the assessment on carbon dioxide removal and insights on enhanced rock weathering, a prediction model is created to provide data support for subsequent implementation of enhanced rock weathering, and/or one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential are determined.\|[0006] In some embodiments, the heavy metal concentration is calculated in response to receiving bio-availability of metals and dissolved aqueous metals. In some embodiments, the soil organic carbon is measured based on determining the loss of material on ignition. In some embodiments, the target is a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling. In some embodiments, the spectroscopy device is a handheld LIBS device. In some embodiments, the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis. In some embodiments, the spectroscopy device is a LIBS device that is combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic from the target.\|[0007] The above and other preferred features, including various novel details of implementation and combination of elements, will now be more particularly described with reference to the accompanying drawings and pointed out in the claims. It will be understood that the particular methods and apparatuses are shown by way of illustration only and not as limitations. As will be understood by those skilled in the art, the principles and features explained herein may be employed in various and numerous embodiments.\|(US20250164404)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0008] The disclosed embodiments have advantages and features which will be more readily apparent from the detailed description, the appended claims, and the accompanying figures (or drawings). A brief introduction of the figures is below.\|[0009] FIG. 1A illustrates a block diagram of an exemplary ERW process.\|[0010] FIG. 1B illustrates a graphic representation of the speciation of a dominant form of dissolved carbon.\|[0011] FIG. 2A illustrates an overview of an exemplary laser induced breakdown spectroscopy (LIBS)-based data system, according to some embodiments.\|[0012] FIG. 2B illustrates an overall diagram of an exemplary LIBS device, according to some embodiments.\|[0013] FIG. 3 illustrates a block diagram of exemplary uses of LIBS devices in an MRV process for ERW, according to some embodiments.\|[0014] FIG. 4 illustrates a block diagram of exemplary features of LIBS devices and analysis used in MRV for ERW described in the present system, according to some embodiments.\|[0015] FIG. 5 illustrates a block diagram of exemplary data analysis and modeling used in the present system, according to some embodiments.\|[0016] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments.\|[0017] FIG. 7 illustrates a block diagram of an example computer system that may be used in implementing the technology described herein, according to some embodiments.\|(US20250164404)\|DETAILED DESCRIPTION\|[0018] The Figures (FIGs.) and the following description relate to preferred embodiments by way of illustration only. It should be noted that from the following discussion, alternative embodiments of the structures and methods disclosed herein will be readily recognized as viable alternatives that may be employed without departing from the principles of what is claimed.\|[0019] Reference will now be made in detail to several embodiments, examples of which are illustrated in the accompanying figures. It is noted that wherever practicable similar or like reference numbers may be used in the figures and may indicate similar or like functionality. The figures depict embodiments of the disclosed system (or method) for purposes of illustration only. One skilled in the art will readily recognize from the following description that alternative embodiments of the structures and methods illustrated herein may be employed without departing from the principles described herein.\|Scientific Introduction\|ERWA—A Durable Carbon Dioxide Removal Strategy\|[0020] Enhanced rock weathering (ERW) is a carbon dioxide removal (CDR) technique where naturally occurring mineral weathering reactions that consume atmospheric CO2 are accelerated. This may be achieved by applying crushed rocks and silicate minerals to agricultural soils. When the gradual rock dissolution or “weathering” occurs, alkaline minerals containing cations, such as calcium and magnesium (Ca2+ and Mg2+) that comprise the silicates, act as a pH amendment to remediate acidic soil on farms. In addition to balancing the pH of the soil, ERW can remove carbon dioxide from the atmosphere and sequester carbon for geological timescales.\|[0021] Basalt can be applied to managed land or an agricultural setting (e.g., rice paddies, corn fields, pasture lands) to practice ERW as a CDR strategy at scale. It should be recognized that the approach described herein is crop agnostic and can be generally applicable to any agricultural or managed land. As the dissolution of basalt proceeds, CO2 gas in the soil is converted to dissolved bicarbonate (HCO3−) in groundwater. This occurs due to basalt weathering reactions involving carbonic acid. Carbonic acid (H2O+CO2═H2CO3) is formed naturally in soils by plant respiration. The conversion of dissolved carbonic acid sources to bicarbonate draws CO2 down from the atmosphere.\|[0022] FIG. 1A illustrates a block diagram 100 of an exemplary ERW process. Basalt and/or other silicate materials (e.g., crushed rocks or “rock powder”) are applied to the soil and mixed into the subsurface near crops in 102. As the ERW progresses, the carbon dioxide (CO2 gas) from the respiration of roots 104 is converted to bicarbonate (HCO3−) in groundwater, and the CO2 stored in the soil 104 is also leached out of the soil and converted to bicarbonate. The bicarbonate is associated with a rising pH value of soil since the soil becomes less acidic. In this way, CO2 is removed. The silicate material application and CO2 isolation are associated with the deposition and sequestration processes 106, which results in the formation of weathering products in surface and groundwater runoff 108. Multiple enhanced rock weathering experiments have also demonstrated significant agronomic benefits due to improved nutrient supply for crops. Therefore, ERW deployments could aid farmers in regions where fertilizers are scarcely available or unaffordable.\|Carbon in Agricultural Setting\|[0023] The behavior of carbon in agricultural settings depends on the pH values in the settings. FIG. 1B illustrates a graphic representation 150 of the speciation of a dominant form of dissolved carbon, specifically, a representative calculation for the speciation of dissolved inorganic carbon (DIC). DIC is the sum of the aqueous species of inorganic carbon in a solution, which includes three major aqueous species: CO2, HCO3−, and CO32−. The speciation of DIC is the distribution of these species in a solution. The speciation of DIC can be determined by measuring the pH and total alkalinity of a solution and then using the measured values to calculate the concentrations of the different DIC species.\|[0024] To obtain the calculation demonstrating how the behavior of DIC changes with the pH value of soil in FIG. 1B, the pH value of the soil and pore waters of rice paddies is shifted towards pH=7 from ERW. As low pH (i.e., acidic) soils transition to neutral pH (i.e., pH≈7 ), dissolved CO2 is converted to the alkaline dissolved mineral bicarbonate (HCO3−). Near PH=7 bicarbonate is the dominant form of DIC. In other words, based on the shifting of the pH value, CO2 is converted to HCO3− and is not released as gas into the atmosphere.\|[0025] Next it is investigated what happens after CO2 is converted to other forms of dissolved inorganic carbon. After the conversion from CO2 to HCO3−, the bicarbonate (HCO3−) percolates into streams and rivers, from where the bicarbonate is delivered to the oceans. This DIC may reside in groundwater within the soil column for decades to centuries. This is an effective removal of carbon dioxide available to the ocean-atmosphere system. The eventual precipitation of bicarbonate as calcium carbonate minerals in deep aquifers or after transport to the ocean stably stores carbon for more than 10,000 years. The delivery of DIC to the ocean in the form of bicarbonate acts to enhance ocean alkalinity, which is vital for the health of ocean flora and fauna. For example, coral ecosystems have been particularly damaged by ocean acidification which is a well-known side effect of climate change. Ocean alkalinity enhancement works to counteract ocean acidification, as shown in 110 of FIG. 1A.\|Technical Problems\|[0026] It is hard to measure carbon capture. In agricultural and forest environments, many methods have been developed for measuring how much carbon is stored in soil. These methods significantly rely on labor-intensive mass-spectrometer measurements, spectroscopy, satellite-based sensors, and modeling. However, understanding the ecosystematic changes in soils is complex, as conditions may vary across a single plot of land. These methods cannot accurately evaluate carbon captured and retained in soils. Most current projects/methods cannot successfully quantify the amount of carbon, much less report carbon sequestration and conservation confidently. These schemes do not help address or incentivize emission avoidance and reduction by high-carbon industries (including agriculture).\|[0027] Even if the issue of carbon measurement can be solved, there are other challenges such as carbon deception. This is another main challenge related to the “net zero” demand in ecosystems. “Net zero” refers to a situation where an amount of carbon dioxide is removed from the atmosphere after that amount of carbon dioxide emission is generated, resulting in zero increase in net emissions. Thus, gas emission is still generated from human activity (e.g., fossil fuel companies can continue to explore, drill, extract, and burn fossil fuels), but carbon dioxide is taken out of the atmosphere in certain ways in some other places to balance out emissions. However dishonest actors may present during this procedure. For example, like a manufacturer rigging vehicles to cheat on emissions tests, forestry interventions may cut trees and then replant trees to claim carbon gains, i.e., carbon deception. Monitoring, reporting, and verification (MRV) is the process that can account for, communicate, and certify a CDR system's carbon removal over time. Currently, ERW lacks a robust MRV framework to obtain proper knowability of carbon sequestration (e.g., detecting carbon deception) and fill the knowledge gap to fulfill the demand of “net zero.”\|[0028] MRV is technically difficult due to the long timescales and uncertainties associated with the chemical and physical processes involved. Some crucial issues in MRV include accurately tracking carbon uptake, ensuring the permanence of carbon storage (e.g., long-time leakage risk), dealing with the variability of the process across different conditions, developing standardized reporting methods that ensure credibility and comparability across projects, etc. For example, there is no feasible way to directly measure the amount of CO2 removed from the atmosphere by ERW, and measuring CO2 in soils and groundwater is inherently challenging due to variability in environmental conditions (e.g., temperature, moisture levels, soil type, microbial activity). Emerging technologies (e.g., remote sensing, advanced soil sampling techniques) and research on effective MRV may help overcome some of the challenges.\|Overview\|[0029] The present disclosure proposes a novel system and method for performing compositional characterization of soil-rock dust mixtures. In some embodiments, the present system includes laser induced breakdown spectroscopy (LIBS) instruments that embody new MRV methodologies for ERW. LIBS deduces the elemental composition of a sample (e.g., solids, liquids, and gases) from measurements of the spectral line emission emitted by the plasma produced by high-power laser irradiation of the sample. LIBS will be described in further detail below.\|[0030] In some embodiments, the proposed workflow as described herein may include four primary facets:\| - i. Choose where to sample and measure compositional characteristics of soils;\| - ii. Determine how to measure compositional characteristics of the soils using LIBS;\| - iii. Analyze LIBS measurements (e.g., based on existing gold-standard measurement techniques); and\| - iv. Use post-processing analytical tools to create high-quality, verifiable carbon credits (a tradable certificate used to reduce global greenhouse gas emissions).\|[0035] The present disclosure also proposes multiple LIBS devices that may be employed in the field, workstations, or laboratories.\|[0036] FIG. 2A illustrates an overview of an exemplary LIBS-based data system 200 that is used to implement the functionalities described herein. In this example, system 200 includes a sample handling unit 202, a LIBS device 204, and a data processing unit 206. System 200 may use sample handling unit 202 to identify locations or zones that target samples (e.g., soil samples) should be collected from (e.g., geolocated zone-based soil sampling). Depending on different quantitative analyses and qualitative analyses to be performed (e.g., as described in FIGS. 3-6), sample handling unit 202 may also be used to instruct LIBS device 204 to obtain specific types of measurements. The present system may further use sample handling unit 202 to ensure the accurate positioning of a sample for optical interaction with LIBS device 204. LIBS device 204 is employed to obtain measurements and analysis data from samples, which will be described in detail in FIG. 2B. The data from LIBS device 204 is further analyzed and modeled by data processing unit 206 for the purpose of monitoring, reporting, and verification, for example, as illustrated in FIG. 5 below. Although only one LIBS device is shown in the example system 200 of FIG. 2A, it is possible that more LIBS devices and/or other units/components may be included in a LIBS-based data system.\|[0037] In some embodiments, at least a portion of the data processing unit 206 is part of a computer system (described below in FIG. 7) that is communicatively coupled to LIBS device 204. In other embodiments, at least a portion of the data processing unit 206 may be integrated into LIBS device 204. For example, data processing unit 206 may reside on a standalone computer system to perform advanced compositional analysis based on real-time sample analysis from data acquisition & analysis component 260 of LIBS device 204 (described below in FIG. 2B). Data processing unit 206 together with data acquisition & analysis component 260 form a data analysis subsystem that is responsible for various types of data processing, evaluation, calculation, etc, as described in the present disclosure. When LIBS device 204 is attached to or mounted on a motor instrument (e.g., vehicle, drone), the data analysis subsystem may be integrated into data acquisition onboard the motor instrument for real-time data acquisition and analysis. In some embodiments, at least a portion of the sample handling unit 202 may also be part of an external computer system and/or an integrated part of LIBS device 204. For example, sample handling unit 202 may be designed to use motorized stages or robots to move a sample in a controlled manner and thus is included in or attached to LIBS device 204 for precise sample positioning.\|LIBS Device\|[0038] LIBS is a rapid chemical analysis technology that uses a short laser pulse to create a micro-plasma on the sample surface. LIBS can be used to detect the presence of various elements in a sample based on directing a high-power emission from a laser onto the sample to form a plasma. The plasma is then analyzed spectroscopically to determine the composition of the sample. The LIBS is often used with a soil penetrating probe to detect heavy metal contamination in soil due to its high sensitivity and sample-free preparation. The LIBS analytical technique offers some other compelling advantages such as fast measurement time (e.g., a few seconds for a single spot analysis), broad elemental coverage (e.g., including, but not limited to, lighter elements such as H, Be, Li, C, N, O, Na, and Mg), versatile sampling protocols that include fast raster of the sample surface and depth profiling, etc.\|[0039] The present disclosure proposes new LIBS device(s) used in the MRV process for ERW. In some embodiments, the new LIBS device is a single multi-purpose optical device. In other embodiments, the new LIBS device may include one or more optical devices. Each device can be designed for a single purpose or multiple purposes. The LIBS devices may have various physical components and/or configurations.\|[0040] FIG. 2B illustrates an overall block diagram of an exemplary LIBS device 204, which includes some key components such as optical source 254, focusing and light collection optics 256, detector 258, and data acquisition & analysis component 260. These components are depicted merely for illustration, and other components (more or less) may be included in LIBS device 204. For example, sample probe 252 may be part of the LIBS device 204. In some embodiments, LIBS device 204 may use a sample probe 252 (e.g., a soil penetrating probe) to take a sample from a target area that is strategically identified (e.g., on managed land). In response, optical source 254 (e.g., a laser) may generate a high-energy light pulse that is directed onto the sample, and focusing and light collection optics 256 (e.g., lens, mirrors) may focus the light pulse to a specific point on the sample, thereby creating a plasma plume. The focusing and light collection optics 256 may also capture/collect the light pulse/beam to avoid light interference. The collected light pulse is then passed through detector 258 (e.g., spectrometer) to obtain sample measurements (e.g., spectral data). For example, detector 258 may disperse the light pulse into individual wavelengths, determine the intensity of light at each wavelength (e.g., using a charge-coupled device (CCD) or photo-multiplier tube (PMT)), and generate a spectrum that is characteristic of specific elements in the sample.\|[0041] Data acquisition & analysis component 260 may include computing hardware such as a central processing unit, memory, and storage, as described in the computer system of FIG. 7. Data acquisition & analysis component 260 is configured to receive the measurement data from detector 258 and perform the elemental composition analysis on the measurement data. In some embodiments, LIBS device 204 may also communicate with an alternative or additional data processing unit (e.g., 206) to perform LIBS analysis and any other elemental identification and quantification analyses. Based on the analysis, a result is generated in 262. For example, the result may be a report or graphical output showing the elemental composition of the sample. Various types of measurements and analyses may be conducted by the data analysis subsystem including data acquisition & analysis component 260 and data processing unit 206, which will be further described below with reference to FIGS. 3-6.\|[0042] The present system may deploy one or more improved LIBS devices to implement the disclosed functionalities. For example, the improved LIBS device (e.g., 204) may be equipped, attached, or associated with an autofocusing component to enable consistent, in-focus measurements of samples without moving other optical components. The autofocusing component may be included as a part of a suitable optical assembly that is hand-held, attached to a mobile vehicle, or integrated with a positioning system (e.g., robotic arm, boom, leg, conveyor belt), etc. Using the autofocusing component, spectroscopy measurements can be automatically focused based on a focal length of its optics relative to the target sample. Instead of using certain mechanisms (e.g., mechanical actuators) to change the position of the optical component(s), in some embodiments, the autofocusing component may include a shape changing lens (e.g., variable focus lens) to allow continuous tuning of a focal length and working distance of the autofocusing component relative to a target sample.\|Data Acquisition and Evaluation Using LIBS Device\|[0043] As discussed above, components 252, 254, 256, 258, and/or 260 of LIBS device 204 may work together with other units of data system 200 to acquire sample data and provide insights about the elemental composition of a sample (e.g., soil sample). In the illustrated embodiment of FIG. 3, one or more LIBS devices 204 may be used to determine weathering status 304, evaluate specific soil contents/elements 306, calculate heavy metal concentration 308, evaluate metal ratios in soils 310, and/or measure soil organic carbon 312. In some embodiments, one or more LIBS devices 200 may also be used to measure and analyze the compositional characteristics of soils, the biological composition of plant and seed matter, and the elemental composition of rock samples.\|[0044] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) used for determining weathering status 304. In some embodiments, a LIBS-based device may be employed to assess the composition of lighter cations relative to heavier cations in applied rock dust. This composition analysis may be used in determining the weathering status of the rock dust application on agricultural fields, pasture lands, or any other natural environments. Thus, an approach is obtained, for determining the loss of rock dust due to enhanced rock weathering (ERW) for the purpose of monitoring, reporting, and verification (MRV) to create carbon credits.\|[0045] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating specific soil elements 306, for example, the nitrogen (N), phosphorus (P), and potassium (K) content of the soil. This is the estimation of nutrient requirements, factoring in additional nutrients provided by rock dust application. The use of LIBS devices in elemental composition analysis can reduce farmers' burden to apply fertilizers (i.e., NPK nitrogen-phosphorus-potassium) while conducting ERW projects. LIBS allows the quantification of these additional bioavailable nutrients, which become active in the soil column with the breakdown of the rock minerals (e.g., being modified through chemical, physical, or biological interactions with rocks and minerals).\|[0046] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for calculating heavy metal concentrations 308, e.g., the amounts of metallic elements (often toxic) found in the soils or rock dust used for ERW. These elements may include metals such as lead (Pb), mercury (Hg), nickel (ni), etc., and can be found in pesticides, fertilizers, or untreated sewage sludge introduced into the soil. The heavy metal may accumulate in the environment to pose serious health and ecological risks. The disclosed LIBS device may provide insights into the safety considerations of cultivating various crops, for example, providing insights into phytoremediation such as using sunflowers to remove Strontium, which is poisonous metal to most other livings. According to US Environmental Protection Agency (EPA) standards, the bio-availability of metals and dissolved aqueous metals will be needed for calculating heavy metal concentrations.\|[0047] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating key metal ratios in soils for ERW 310. In some embodiments, critical metal ratios in soils are assessed using LIBS technology before the implementation of ERW (i.e., before the rock dust application for enhanced weathering). This process can be outlined as follows:\| - i. Sample Collection: soil samples are collected from the target area where ERW is planned. These samples represent the current soil composition in the region;\| - ii. LIBS Analysis: the collected soil samples are subjected to LIBS analysis. The LIBS device measures the elemental composition of the soil, providing baseline data on the concentrations of various metals being present;\| - iii. Trace metal ratios and potential pulverized rock dust field amendments may then be evaluated together to determine if the rock dust is appropriate for application to the field; and \| - a. Evaluate environmental concerns,\| - b. Evaluate the potential for signal strength in measurements: measuring key metal ratios for MRV process.\| - iv. Key Metal Ratios: specific metal ratios of interest, which are known to influence the effectiveness of ERW, are calculated based on the LIBS data. These key metal ratios often include ratios such as calcium to magnesium (Ca/Mg), calcium to potassium (Ca/K), or calcium to sodium (Ca/Na), among others.\|[0054] In some embodiments, the calculated key metal ratios are evaluated to determine the suitability of the soil for ERW. An ideal balance of these ratios is typically necessary for optimal carbon capture and weathering outcomes. The assessment results may guide decisions regarding the need for rock dust application and the specific rock dust type required to achieve the desired metal ratios for effective ERW.\|[0055] By employing LIBS technology for the evaluation of key metal ratios in soils before rock dust application for enhanced weathering, informed decision-making can be used to ensure that the chosen ERW strategy is tailored to the specific soil composition of the target area. This optimization may also contribute to efficient carbon dioxide removal and MRV.\|[0056] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for measuring soil organic carbon 312. A LIBS device can be used to measure soil organic carbon (SOC) levels. The SOC level represents the amount of carbon stored in the form of organic compounds in the soil, and SOC is critical to soil quality and carbon sequestration because it helps store carbon from the atmosphere and contributes to mitigating climate change. By measuring the SOC level, the present disclosure facilitates the correlation between changes in organic carbon attributable to rock dust application, thereby offering valuable insights into soil improvement. In some embodiments, soil organic carbon measurements may be approximated by the loss of material on ignition (LOI) (e.g., by measuring the weight loss of organic matter content after heating the sample to a high temperature).\|LIBS Analysis\|[0057] Numerous LIBS analyses may be conducted based on element measurements, calculation, and evaluation. In addition to in-depth soil analysis, when a LIBS device is used to measure the biological composition of plant and seed matter, the LIBS analysis can serve to validate the absence of potential metal accumulation resulting from enhanced weathering processes.\|[0058] In some embodiments, a LIBS device may also be used for rock sample analysis, where the elemental composition of raw rock samples from rock quarries or in the field is analyzed. This LIBS analysis may be applied to determine an enhanced weathering potential and a total carbon dioxide removal (CDR) potential. The enhanced weathering potential is the amount of atmospheric carbon dioxide that can be removed and stored through the ERW process (e.g., manual application of rocks or minerals) over a specific period of time. This factor may vary depending on the type of rocks/minerals used in ERW, the surface area available for reaction, environmental conditions (e.g., precipitation, temperature), etc. The total CDR potential is the amount of carbon dioxide that can be removed from the atmosphere in the long term, which depends on the effectiveness of the ERW process.\|[0059] In some embodiments, a spectral fluorescence device may be used in combination with LIBS analysis to create a dual system. This dual system enables the simultaneous determination of organic carbon and elemental composition in samples. This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status. In some embodiments, this approach may also be used to help refine soil organic carbon estimates outlined in 312 of FIG. 3. In general, the combination of LIBS and fluorescence may expand and strengthen the LIBS measurement and analysis, e.g., as discussed in FIG. 3.\|Beneficial Features of LIBS Device and Analysis\|[0060] FIG. 4 illustrates a block diagram 400 of exemplary features of LIBS devices and analysis used in the MRV process for ERW as described in the present system.\|[0061] The present system allows improved statistical accuracy with pooled/composite soil samples, as shown in 402. By aggregating soil samples from various locations within a field, the present system seeks to accurately determine the central compositional tendency and associated dispersion or variance in the soil's elemental composition. As compared to the current techniques, the utilization of pooled samples enables a more robust and representative analysis of the soil's overall composition, contributing to a more precise assessment of soil quality and environmental conditions. The accurate measurement of pooled samples is particularly important to soil fertility assessment, soil quality monitoring, and precision agriculture.\|[0062] The present system provides geolocated zone-based soil sampling for target characteristic assessment, as shown in 404. In some embodiments, the present system allows the collection of soil samples from specific geolocated zones within a field. By strategically pooling samples from these distinct zones, the analysis can yield precise data regarding the central tendency and variance of the target characteristic within each zone. This geolocated zone-based sampling approach offers a granular understanding of the spatial heterogeneity, distribution, and variability of the target characteristic, thereby enabling informed decision-making for soil management and ERW applications. Potential future obstacles with a MRV process based on soil heterogeneity may also be addressed by examining measurements at this juncture. In some embodiments, zones may be determined based on soil type, gridded areas, etc. A zone may also be small, predefined regions that include, but are not limited to, a circular region with a predefined radius or a square area with a predefined side length.\|[0063] The LIBS device of the present system can be used in rock sample analysis to determine enhanced weathering potential and total carbon dioxide removal (CDR) potential. In particular, the present system may evaluate the carbon dioxide potential of alkaline silicate minerals, as shown in 406. The present system can assess the carbon dioxide potential of alkaline silicate minerals including, but not limited to, basalt, olivine, and wollastonite. These minerals are known for their capacity to sequester carbon dioxide through enhanced weathering processes. In some embodiments, the present system may utilize a LIBS device to analyze the elemental composition of these minerals and determine their specific potential for CDR. By accurately quantifying the CDR potential of alkaline silicate minerals, the present system gains valuable insights into the efficacy of a CDR solution.\|[0064] The present system allows systematic preparation of pressed-pelletized subsamples derived from pooled soil samples, as shown in 408. By compressing and pelletizing soil material from each pooled sample, the present system may create a consistent and standardized substrate for LIBS analysis. This process can minimize variations in sample presentation, ensuring reliable and reproducible results during LIBS analysis. This process further streamlines the handling of samples, allowing for an efficient assessment of the central compositional tendency and variance of the target characteristics within the soil, and ultimately enhancing the accuracy of soil quality and environmental assessments.\|[0065] The present system further allows grid-based or rastered LIBS sampling for in-depth soil core analysis, as shown in 410. In some embodiments, the present system may conduct grid-based or rastered analyses of the pelletized subsamples, where the LIBS device systematically scans and analyzes discrete regions or points on the pellet surface in a structured grid or raster pattern. This approach enables a comprehensive examination of the intersample heterogeneity (or microheterogeneity) of soil characteristics and the distribution of elemental composition within the subsamples.\|[0066] Through this analysis, the present system may achieve a high-resolution understanding of the central compositional tendency and variance of the target characteristics in the soil, and the detailed information may provide invaluable insights into the spatial variability of soil properties, thereby enhancing precision in soil quality assessment and MRV for CDR applications.\|[0067] Using rasterized or gridded LIBS sampling can also systematically measure the elemental composition of intact soil cores at various depths. By taking measurements in a prescribed structured grid or raster pattern for LIBS analysis along the length of an intact soil core, the present approach enables precise characterization of the compositional variations with depth. This is particularly beneficial for understanding how soil properties change at different depths within the core, offering crucial insights into subsurface composition and environmental conditions. The present system seeks to assess soil heterogeneity and geological attributes with depth, contributing to informed decisions in ERW applications and MRV techniques.\|Device Characteristics and Deployment\|[0068] The present system supports specific device characteristics and deployment that are beneficial to the MRV process for ERW. In some embodiments, the present system supports handheld and miniaturized LIBS devices for soil sampling, field-based depth-integrated soil profiling with LIBS and soil auger, and in-field deployment of LIBS technology on motor vehicles, etc.\|[0069] The LIBS device described herein can be a handheld device that is portable, easy to operate, and suitable for rapid data acquisition. This handheld device is particularly useful in patchwork small-holder farms (e.g., rice paddies). It is engineered to provide a simplified user interface while maintaining the analytical accuracy and precision required for soil and environmental analysis. Any instantiation of the LIBS device may contain fewer optical sensors than the original, making the device more affordable and lighter. As a result, this LIBS device is adaptive for use in rural, remote, and economically disadvantaged communities. In addition, the miniaturized form of the device enables the present system to perform real-time, in-situ analyses, contributing to timelier and data-driven decision-making processes in agriculture, geology, and environmental science.\|[0070] The present system also allows a LIBS device to be combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic. A soil auger is employed to collect soil samples at various depths within the field. These samples are representative of the soil composition at specific depth intervals.\|[0071] After and/or during the auguring process, the present system performs LIBS analysis on the collected soil samples. A LIBS device can rapidly and accurately measure the elemental composition of the soil samples, including the concentration of the target characteristic of interest. The present system may then integrate the LIBS data obtained from each depth interval to construct a depth-integrated soil profile of the target characteristic. This profile provides a comprehensive understanding of how the target characteristic varies with depth within the soil.\|[0072] A LIBS device/instrument can be deployed in different ways. In some embodiments, the present system supports in-field deployment of LIBS technology on motor vehicles. LIBS is integrated into motor vehicles, such as tractors or other agricultural machinery, for in-field deployment. The present system seamlessly integrates LIBS instrumentation into the design of motor vehicles used for field operations, such as tractors.\|[0073] The LIBS device can be securely mounted, ensuring stability during vehicle movement. The LIBS device may operate in real time as the motor vehicle traverses the field. The LIBS device continuously analyzes the soil or other target materials as the vehicle moves, providing instant elemental composition data. The present system may collect LIBS-generated data and integrate the data into a data acquisition (DAQ) onboard the vehicle, allowing for real-time decision-making based on soil or material composition. A vehicle operator can use the LIBS data to make immediate adjustments to field operations for any ERW-related purpose, such as varying fertilizer application rates or adjusting rock dust application rates based on the in-field analysis. The present system may log the LIBS data, providing a detailed record of the soil or material composition across the field for subsequent analysis and optimization.\|[0074] In some embodiments, the present system may support other deployment methods. For example, one or more LIBS devices may be integrated into drones, underwater vehicles/amphibious, or other mobil instruments.\|Data Analysis and Modeling\|[0075] FIG. 5 illustrates a block diagram 500 of exemplary features of data analysis and modeling used in the present system. As depicted in FIG. 5, the data analysis and modeling 502 of the present system may be featured with various analytical tools such as multivariate distribution modeling for cation covariance analysis 504, empirical modeling for weathering prediction and carbon credit creation 506, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data 508, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS 510, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV 512. In some embodiments, these data analyses and modeling may be performed at least by data processing unit 206 in combination with data acquisition & analysis component 260 as shown in FIGS. 2A and 2B (i.e., data analysis subsystem).\|[0076] The present system provides multivariate distribution modeling for cation covariance analysis, as shown in 504. In some embodiments, the LIBS data can be leveraged for analyzing and modeling the covariance relationships among key cations in soil including, but not limited to, titanium, calcium, sodium, magnesium, potassium, phosphorous, and nitrogen. In some embodiments, the present system entails fitting multivariate normal or non-normal distributions to the data obtained through LIBS measurements.\|[0077] Multivariate distribution fitting allows for the comprehensive assessment of the covariance and correlations between key cations in soil. It provides valuable insights into the simultaneous variations and relationships among these elements, contributing to a deep understanding of soil composition and baseline information required for MRV. The present system uses LIBS to provide dense and rapid enough data to find systematic variances in soil heterogeneity within any given field, pasture, agricultural setting, or any other natural setting.\|[0078] In some embodiments, the present system may apply the quantitative elemental analysis approach as described in Sobron, titled “non-linear methods for quantitative elemental analysis and mineral classification using laser-induced breakdown spectroscopy (LIBS),” U.S. patent application Ser. No. 15/998,391, which is hereby incorporated by reference in its entirety.\|[0079] In some embodiments, the present system supports empirical modeling for weathering prediction and carbon credit creation, as shown in 406. That is, data collected in the present system can be leveraged to develop an empirically driven model for predicting the weathering of rock dust applied to fields and providing suggestions and instructions for subsequent ERW implementation.\|[0080] The empirical model may help the monitoring, reporting, and verification (MRV) process, which aims at quantifying the carbon capture potential resulting from enhanced weathering practices. By using dense, LIBS-generated data to create a predictive model, it becomes possible to monitor and report on the efficiency of carbon capture using regression-based and/or machine-learning methods. As a result, the time between data collection and sales for creating carbon credits may be reduced. The empirically driven model therefore facilitates accurate and data-driven MRV processes while incentivizing an easy switch to practices where carbon credits may be created through ERW. For example, when structure a predictive model, the present system may use mineral type, application rate, surface area of mineral, climate data, and environmental carbon dioxide concentration as input parameters of the model. The present system may calculate the weathering rate based on the environmental conditions and mineral properties, calculate the sequestration of carbon dioxide, and use weathering rate equations to predict how much carbon dioxide may be captured within a specific area over a specific timeframe. The present system may also calculate the total carbon dioxide removal rate to estimate global or regional carbon dioxide sequestration potential.\|[0081] To ensure accuracy and precision, in some embodiments, the present system may calibrate the LIBS device using high-precision measurements obtained from ICP-MS, as shown in 508.\|[0082] ICP-MS represents a well-established and highly accurate analytical technique, known for its exceptional precision in measuring elemental composition. By calibrating the LIBS device against ICP-MS data, the present system may establish a robust and reliable calibration framework. This calibration method may serve to validate and fine-tune the LIBS measurements, ensuring accuracy and traceability to a gold standard in elemental analysis.\|[0083] The integration of ICP-MS calibration in the present system enhances the trustworthiness and consistency of LIBS measurements, and the enhanced measurements may be suitable for a wide range of ERW applications for MRV. This calibration approach boosts the credibility of LIBS technology in scientific research and regulatory compliance (e.g., metals contamination according to EPA standards).\|[0084] The present system supports the construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, as shown in 510. In some embodiments, the present system may use known mixtures of soil and rock dust to create calibration curves. With a soil sample and rock dust sample that have already been characterized via ICP-MS or other analytical techniques, the present system can obtain known mixtures such that the rock dust comprises a known percentage of the weight of a newly created sample. By testing many mixed samples using LIBS with an array of rock dust ranging from 0 to 100% weight by mass, the present system can determine a series of calibration curves. These curves may fit the compositional characteristics of a particular soil type-rock dust combination. The present system may then store the data for soil type-rock dust combinations, creating a large database of possible LIBS spectral signals for a range of possible compositional arrays. With a sufficiently large database, the present system can apply one or more regression-based, machine-learning-based tools, and principal component analysis to select the most optimal calibration curve for new measurement(s).\|[0085] Here, the present system aims to strengthen the credibility of carbon credit generation. In some embodiments, the present system may use the misfit of measurements to known calibration curves to quantify measurement uncertainty, so that carbon credit sales effectively incorporate potential variations in carbon capture into pricing structures.\|[0086] In some embodiments, the present system supports collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV, as shown in 512. In other words, ICP-MS and LIBS are used collaboratively to spot-check and validate the empirically driven model developed for CDR MRV. This process ensures that the model accurately reflects the carbon capture and sequestration processes in real-world applications, enhancing the reliability of carbon credit generation. The present system may also use the same collaborative framework to generate uncertainty models when upscaling the sample area for MRV. To upscale the sample area for MRV, test plots are used to make projections for larger fields, and/or several fields are used to project CDR for a region, etc. By systematically assessing variations and uncertainties using ICP-MS and LIBS data, these models provide insights into the potential variability in carbon capture estimates as the sample area is expanded. This information is essential for accurately quantifying carbon credits and assuaging buyers' concerns about the quality of carbon credits. The information is also crucial to assess the quality of MRV.\|[0087] The present system aims to strengthen the credibility of carbon credit generation and improve informed decision-making in ERW-related land management. By integrating uncertainty modeling, the present system enhances its ability to account for variations in carbon capture and carbon dioxide removal potential and provides a comprehensive assessment of carbon dioxide removal efforts. The present system may enhance the credibility of carbon credit generation while providing transparency and accountability in environmental initiatives.\|Flowchart\|[0088] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments. Method 600 may be implemented using a LIBS-based data system 200, as shown in FIGS. 2A and 2B. A spectroscopy device (e.g., LIBS device 204) is used to obtain measurements from a target sample. At step 602, the spectroscopy device (e.g., using optical source 254) emits one or more optical signals directed to a target collected from a target area (e.g., managed field or other agricultural settings). At step 604, the spectroscopy device (e.g., using detector 258) determines spectral measurements of the optical signals collected from the target. The target can be a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified (e.g., by sample handing unit 202) from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered LIBS sampling.\|[0089] As shown in FIGS. 2A and 2B, a data analysis subsystem (e.g., including data processing unit 206 and data acquisition & analysis component 260) is communicatively coupled to the spectroscopy device (e.g., LIBS device 204). At step 606, the data analysis subsystem is configured to convert the spectral measurements to data indicating compositional characteristics of the target, which includes at least one or more of determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. For example, to determine the weathering status, loss of rock dust may be determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering.\|[0090] The data analysis subsystem is then configured to analyze the data indicating compositional characteristics of the target using a plurality of analytical tools at step 608, and provide assessment on carbon dioxide removal and insights on enhanced rock weathering at step 610. In some embodiments, to analyze the compositional data, the data analysis subsystem uses various analytical tools to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision ICP-MS data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS, etc. To provide the assessment, the data analysis subsystem may also calculate one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.\|Computer Implementation\|[0091] In some examples, some or all of the processing described above can be carried out on a personal computing device, on one or more centralized computing devices, or via cloud-based processing by one or more servers. Some types of processing can occur on one device and other types of processing can occur on another device. Some or all of the data described above can be stored on a personal computing device, in data storage hosted on one or more centralized computing devices, and/or via cloud-based storage. Some data can be stored in one location and other data can be stored in another location. In some examples, quantum computing can be used, and/or functional programming languages can be used. Electrical memory, such as flash-based memory, can be used.\|[0092] FIG. 7 is a block diagram of an example computer system 700 that may be used in implementing the technology described herein. General-purpose computers, network appliances, mobile devices, or other electronic systems may also include at least portions of the system 700. The system 700 includes a processor 710, a memory 720, a storage device 730, and an input/output device 740. Each of the components 710, 720, 730, and 740 may be interconnected, for example, using a system bus 750. The processor 710 is capable of processing instructions for execution within the system 700. In some implementations, the processor 710 is single-threaded. In some implementations, the processor 710 is a multi-threaded processor. The processor 710 is capable of processing instructions stored in the memory 720 or on the storage device 730.\|[0093] Memory 720 stores information within the system 700. In some implementations, the memory 720 is a non-transitory computer-readable medium. In some implementations, the memory 720 is a volatile memory unit. In some implementations, the memory 720 is a non-volatile memory unit.\|[0094] The storage device 730 is capable of providing mass storage for the system 700. In some implementations, the storage device 730 is a non-transitory computer-readable medium. In various implementations, the storage device 730 may include, for example, a hard disk device, an optical disk device, a solid-state drive, a flash drive, or some other large-capacity storage device. For example, the storage device may store long-term data (e.g., database data, file system data, etc.). The input/output device 740 provides input/output operations for the system 700. In some implementations, the input/output device 740 may include one or more network interface devices, e.g., an Ethernet card, a serial communication device, e.g., an RS-232 port, and/or a wireless interface device, e.g., an 802.11 card, a 3G wireless modem, or a 4G wireless modem. In some implementations, the input/output device may include driver devices configured to receive input data and send output data to other input/output devices, e.g., keyboard, printer, and display devices 760. In some examples, mobile computing devices, mobile communication devices, and other devices may be used.\|[0095] In some implementations, at least a portion of the approaches described above may be realized by instructions that upon execution cause one or more processing devices to carry out the processes and functions described above. Such instructions may include, for example, interpreted instructions such as script instructions, executable code, or other instructions stored in a non-transitory computer-readable medium. The storage device 730 may be implemented in a distributed way over a network, such as a server farm or a set of widely distributed servers, or may be implemented in a single computing device.\|[0096] Although an example processing system has been described in FIG. 7, embodiments of the subject matter, functional operations, and processes described in this specification can be implemented in other types of digital electronic circuitry, in tangibly embodied computer software or firmware, in computer hardware, including the structures disclosed in this specification and their structural equivalents, or in combinations of one or more of them. Embodiments of the subject matter described in this specification can be implemented as one or more computer programs, i.e., one or more modules of computer program instructions encoded on a tangible nonvolatile program carrier for execution by, or to control the operation of, data processing apparatus. Alternatively or in addition, the program instructions can be encoded on an artificially generated propagated signal, e.g., a machine-generated electrical, optical, or electromagnetic signal that is generated to encode information for transmission to a suitable receiver apparatus for execution by a data processing apparatus. The computer storage medium can be a machine-readable storage device, a machine-readable storage substrate, a random or serial access memory device, or a combination of one or more of them.\|[0097] The term “system” may encompass all kinds of apparatus, devices, and machines for processing data, including by way of example a programmable processor, a computer, or multiple processors or computers. A processing system may include special-purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit). A processing system may include, in addition to hardware, code that creates an execution environment for the computer program in question, e.g., code that constitutes processor firmware, a protocol stack, a database management system, an operating system, or a combination of one or more of them.\|[0098] A computer program (which may also be referred to or described as a program, software, a software application, a module, a software module, a script, or code) can be written in any form of programming language, including compiled or interpreted languages, or declarative or procedural languages, and it can be deployed in any form, including as a standalone program or as a module, component, subroutine, or other unit suitable for use in a computing environment. A computer program may, but need not, correspond to a file in a file system. A program can be stored in a portion of a file that holds other programs or data (e.g., one or more scripts stored in a markup language document), in a single file dedicated to the program in question, or in multiple coordinated files (e.g., files that store one or more modules, sub programs, or portions of code). A computer program can be deployed to be executed on one computer or on multiple computers that are located at one site or distributed across multiple sites and interconnected by a communication network.\|[0099] The processes and logic flows described in this specification can be performed by one or more programmable computers executing one or more computer programs to perform functions by operating on input data and generating output. The processes and logic flows can also be performed by, and apparatus can also be implemented as, special purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit).\|[0100] Computers suitable for the execution of a computer program can include, by way of example, general or special purpose microprocessors or both, or any other kind of central processing unit. Generally, a central processing unit will receive instructions and data from a read-only memory, a random access memory, or both. A computer generally includes a central processing unit for performing or executing instructions and one or more memory devices for storing instructions and data. Generally, a computer will also include, or be operatively coupled to receive data from or transfer data to, or both, one or more mass storage devices for storing data, e.g., magnetic, magneto-optical disks, or optical disks. However, a computer need not have such devices. Moreover, a computer can be embedded in another device, e.g., a mobile telephone, a personal digital assistant (PDA), a mobile audio or video player, a game console, a Global Positioning System (GPS) receiver, or a portable storage device (e.g., a universal serial bus (USB) flash drive), to name just a few.\|[0101] Computer-readable media suitable for storing computer program instructions and data include all forms of non-volatile memory, media, and memory devices, including by way of example semiconductor memory devices, e.g., EPROM, EEPROM, and flash memory devices; magnetic disks, e.g., internal hard disks or removable disks; magneto-optical disks; and CD-ROM and DVD-ROM disks. The processor and the memory can be supplemented by, or incorporated in special-purpose logic circuitry.\|[0102] To provide for interaction with a user, embodiments of the subject matter described in this specification can be implemented on a computer having a display device, e.g., a CRT (cathode ray tube) or LCD (liquid crystal display) monitor, for displaying information to the user and a keyboard and a pointing device, e.g., a mouse or a trackball, by which the user can provide input to the computer. Other kinds of devices can be used to provide for interaction with a user as well; for example, feedback provided to the user can be any form of sensory feedback, e.g., visual feedback, auditory feedback, or tactile feedback; and input from the user can be received in any form, including acoustic, speech, or tactile input. In addition, a computer can interact with a user by sending documents to and receiving documents from a device that is used by the user; for example, by sending web pages to a web browser on a user's user device in response to requests received from the web browser.\|[0103] Embodiments of the subject matter described in this specification can be implemented in a computing system that includes a back-end component, e.g., as a data server, or that includes a middleware component, e.g., an application server, or that includes a front-end component, e.g., a client computer having a graphical user interface or a Web browser through which a user can interact with an implementation of the subject matter described in this specification, or any combination of one or more such back end, middleware, or front end components. The components of the system can be interconnected by any form or medium of digital data communication, e.g., a communication network. Examples of communication networks include a local area network (“LAN”) and a wide area network (“WAN”), e.g., the Internet.\|[0104] The computing system can include clients and servers. A client and server are generally remote from each other and typically interact through a communication network. The relationship between client and server arises by virtue of computer programs running on the respective computers and having a client-server relationship with each other.\|[0105] While this specification contains many specific implementation details, these should not be construed as limitations on the scope of what may be claimed, but rather as descriptions of features that may be specific to particular embodiments. Certain features that are described in this specification in the context of separate embodiments can also be implemented in combination in a single embodiment. Conversely, various features that are described in the context of a single embodiment can also be implemented in multiple embodiments separately or in any suitable sub-combination. Moreover, although features may be described above as acting in certain combinations and even initially claimed as such, one or more features from a claimed combination can in some cases be excised from the combination, and the claimed combination may be directed to a sub-combination or variation of a sub-combination.\|[0106] Similarly, while operations are depicted in the drawings in a particular order, this should not be understood as requiring that such operations be performed in the particular order shown or in sequential order, or that all illustrated operations be performed, to achieve desirable results. In certain circumstances, multitasking and parallel processing may be advantageous. Moreover, the separation of various system components in the embodiments described above should not be understood as requiring such separation in all embodiments, and it should be understood that the described program components and systems can generally be integrated together in a single software product or packaged into multiple software products.\|[0107] Particular embodiments of the subject matter have been described. Other embodiments are within the scope of the following claims. For example, the actions recited in the claims can be performed in a different order and still achieve desirable results. As one example, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In certain implementations, multitasking and parallel processing may be advantageous. Other steps or stages may be provided, or steps or stages may be eliminated, from the described processes. Accordingly, other implementations are within the scope of the following claims.\|Terminology\|[0108] The phraseology and terminology used herein are for the purpose of description and should not be regarded as limiting.\|[0109] The term “approximately”, the phrase “approximately equal to”, and other similar phrases, as used in the specification and the claims (e.g., “X has a value of approximately Y” or “X is approximately equal to Y”), should be understood to mean that one value (X) is within a predetermined range of another value (Y). The predetermined range may be plus or minus 20%, 10%, 5%, 3%, 1%, 0.1%, or less than 0.1%, unless otherwise indicated.\|[0110] The indefinite articles “a” and “an,” as used in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.” The phrase “and/or,” as used in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Multiple elements listed with “and/or” should be construed in the same fashion, i.e., “one or more” of the elements so conjoined. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, a reference to “A and/or B”, when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A only (optionally including elements other than B); in another embodiment, to B only (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc.\|[0111] As used in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of,” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of,” “only one of,” or “exactly one of.” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law.\|[0112] As used in the specification and in the claims, the phrase “at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements. This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase “at least one” refers, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, “at least one of A and B” (or, equivalently, “at least one of A or B,” or, equivalently “at least one of A and/or B”) can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc.\|[0113] The use of “including,” “comprising,” “having,” “containing,” “involving,” and variations thereof, is meant to encompass the items listed thereafter and additional items.\|[0114] Use of ordinal terms such as “first,” “second,” “third,” etc., in the claims to modify a claim element does not by itself connote any priority, precedence, or order of one claim element over another or the temporal order in which acts of a method are performed. Ordinal terms are used merely as labels to distinguish one claim element having a certain name from another element having a same name (but for use of the ordinal term), to distinguish the claim elements.\|[0115] Each numerical value presented herein, for example, in a table, a chart, or a graph, is contemplated to represent a minimum value or a maximum value in a range for a corresponding parameter. Accordingly, when added to the claims, the numerical value provides express support for claiming the range, which may lie above or below the numerical value, in accordance with the teachings herein. Absent inclusion in the claims, each numerical value presented herein is not to be considered limiting in any regard.\|[0116] The terms and expressions employed herein are used as terms and expressions of description and not of limitation, and there is no intention, in the use of such terms and expressions, of excluding any equivalents of the features shown and described or portions thereof. In addition, having described certain embodiments of the invention, it will be apparent to those of ordinary skill in the art that other embodiments incorporating the concepts disclosed herein may be used without departing from the spirit and scope of the invention. The features and functions of the various embodiments may be arranged in various combinations and permutations, and all are considered to be within the scope of the disclosed invention. Accordingly, the described embodiments are to be considered in all respects as only illustrative and not restrictive. Furthermore, the configurations, materials, and dimensions described herein are intended as illustrative and in no way limiting. Similarly, although physical explanations have been provided for explanatory purposes, there is no intent to be bound by any particular theory or mechanism, or to limit the claims in accordance therewith.	(US20250164404)\|CROSS REFERENCE TO RELATED APPLICATION\|[0001] This application claims the benefit of U.S. Provisional Patent Application No. 63/601,059, titled “System and Method for Enhanced Rock Weathering Monitoring, Reporting, and Verification,” and filed on Nov. 20, 2023, the entire content of which is incorporated by reference herein.\|(US20250164404)\|TECHNICAL FIELD\|[0002] This disclosure relates to compositional characterization techniques, in particular, to optical devices that embody new methodologies for monitoring, reporting, and verification (MRV) of enhanced rock weathering (ERW).\|BACKGROUND\|[0003] Enhanced rock weathering (ERW) is the practice of applying crushed rocks and silicate minerals to agricultural land. It is a promising scalable and cost-effective carbon dioxide removal (CDR) strategy with significant environmental and agronomic co-benefits. However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions. Most current projects/systems/devices cannot accurately obtain carbon measurement and properly report carbon sequestration. Also, ERW lacks a robust monitoring, reporting, and verification (MRV) framework to address challenging problems such as carbon deception. For example, current MRV practices cannot provide a framework to easily detect and process a fraudulent claim of carbon gains by dishonest actors in the system.\|SUMMARY\|[0004] To address the aforementioned shortcomings, a method and a system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. The method include using a spectroscopy device to emit one or more optical signals directed to a target collected from a target area and to determine spectral measurements of the optical signals collected from the target. The method also includes using a data analysis subsystem to convert the spectral measurements to data indicating compositional characteristics of the target, analyze the data indicating compositional characteristics of the target using a plurality of analytical tools, and provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\|[0005] To convert the spectral measurements to the data indicating compositional characteristics of the target, one or more of the processes, such as determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. To determine the weathering status, loss of rock dust is determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering. To analyze the data indicating compositional characteristics, analytical tools are used to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS. To provide the assessment on carbon dioxide removal and insights on enhanced rock weathering, a prediction model is created to provide data support for subsequent implementation of enhanced rock weathering, and/or one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential are determined.\|[0006] In some embodiments, the heavy metal concentration is calculated in response to receiving bio-availability of metals and dissolved aqueous metals. In some embodiments, the soil organic carbon is measured based on determining the loss of material on ignition. In some embodiments, the target is a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling. In some embodiments, the spectroscopy device is a handheld LIBS device. In some embodiments, the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis. In some embodiments, the spectroscopy device is a LIBS device that is combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic from the target.\|[0007] The above and other preferred features, including various novel details of implementation and combination of elements, will now be more particularly described with reference to the accompanying drawings and pointed out in the claims. It will be understood that the particular methods and apparatuses are shown by way of illustration only and not as limitations. As will be understood by those skilled in the art, the principles and features explained herein may be employed in various and numerous embodiments.\|(US20250164404)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0008] The disclosed embodiments have advantages and features which will be more readily apparent from the detailed description, the appended claims, and the accompanying figures (or drawings). A brief introduction of the figures is below.\|[0009] FIG. 1A illustrates a block diagram of an exemplary ERW process.\|[0010] FIG. 1B illustrates a graphic representation of the speciation of a dominant form of dissolved carbon.\|[0011] FIG. 2A illustrates an overview of an exemplary laser induced breakdown spectroscopy (LIBS)-based data system, according to some embodiments.\|[0012] FIG. 2B illustrates an overall diagram of an exemplary LIBS device, according to some embodiments.\|[0013] FIG. 3 illustrates a block diagram of exemplary uses of LIBS devices in an MRV process for ERW, according to some embodiments.\|[0014] FIG. 4 illustrates a block diagram of exemplary features of LIBS devices and analysis used in MRV for ERW described in the present system, according to some embodiments.\|[0015] FIG. 5 illustrates a block diagram of exemplary data analysis and modeling used in the present system, according to some embodiments.\|[0016] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments.\|[0017] FIG. 7 illustrates a block diagram of an example computer system that may be used in implementing the technology described herein, according to some embodiments.\|(US20250164404)\|DETAILED DESCRIPTION\|[0018] The Figures (FIGs.) and the following description relate to preferred embodiments by way of illustration only. It should be noted that from the following discussion, alternative embodiments of the structures and methods disclosed herein will be readily recognized as viable alternatives that may be employed without departing from the principles of what is claimed.\|[0019] Reference will now be made in detail to several embodiments, examples of which are illustrated in the accompanying figures. It is noted that wherever practicable similar or like reference numbers may be used in the figures and may indicate similar or like functionality. The figures depict embodiments of the disclosed system (or method) for purposes of illustration only. One skilled in the art will readily recognize from the following description that alternative embodiments of the structures and methods illustrated herein may be employed without departing from the principles described herein.\|Scientific Introduction\|ERWA—A Durable Carbon Dioxide Removal Strategy\|[0020] Enhanced rock weathering (ERW) is a carbon dioxide removal (CDR) technique where naturally occurring mineral weathering reactions that consume atmospheric CO2 are accelerated. This may be achieved by applying crushed rocks and silicate minerals to agricultural soils. When the gradual rock dissolution or “weathering” occurs, alkaline minerals containing cations, such as calcium and magnesium (Ca2+ and Mg2+) that comprise the silicates, act as a pH amendment to remediate acidic soil on farms. In addition to balancing the pH of the soil, ERW can remove carbon dioxide from the atmosphere and sequester carbon for geological timescales.\|[0021] Basalt can be applied to managed land or an agricultural setting (e.g., rice paddies, corn fields, pasture lands) to practice ERW as a CDR strategy at scale. It should be recognized that the approach described herein is crop agnostic and can be generally applicable to any agricultural or managed land. As the dissolution of basalt proceeds, CO2 gas in the soil is converted to dissolved bicarbonate (HCO3−) in groundwater. This occurs due to basalt weathering reactions involving carbonic acid. Carbonic acid (H2O+CO2═H2CO3) is formed naturally in soils by plant respiration. The conversion of dissolved carbonic acid sources to bicarbonate draws CO2 down from the atmosphere.\|[0022] FIG. 1A illustrates a block diagram 100 of an exemplary ERW process. Basalt and/or other silicate materials (e.g., crushed rocks or “rock powder”) are applied to the soil and mixed into the subsurface near crops in 102. As the ERW progresses, the carbon dioxide (CO2 gas) from the respiration of roots 104 is converted to bicarbonate (HCO3−) in groundwater, and the CO2 stored in the soil 104 is also leached out of the soil and converted to bicarbonate. The bicarbonate is associated with a rising pH value of soil since the soil becomes less acidic. In this way, CO2 is removed. The silicate material application and CO2 isolation are associated with the deposition and sequestration processes 106, which results in the formation of weathering products in surface and groundwater runoff 108. Multiple enhanced rock weathering experiments have also demonstrated significant agronomic benefits due to improved nutrient supply for crops. Therefore, ERW deployments could aid farmers in regions where fertilizers are scarcely available or unaffordable.\|Carbon in Agricultural Setting\|[0023] The behavior of carbon in agricultural settings depends on the pH values in the settings. FIG. 1B illustrates a graphic representation 150 of the speciation of a dominant form of dissolved carbon, specifically, a representative calculation for the speciation of dissolved inorganic carbon (DIC). DIC is the sum of the aqueous species of inorganic carbon in a solution, which includes three major aqueous species: CO2, HCO3−, and CO32−. The speciation of DIC is the distribution of these species in a solution. The speciation of DIC can be determined by measuring the pH and total alkalinity of a solution and then using the measured values to calculate the concentrations of the different DIC species.\|[0024] To obtain the calculation demonstrating how the behavior of DIC changes with the pH value of soil in FIG. 1B, the pH value of the soil and pore waters of rice paddies is shifted towards pH=7 from ERW. As low pH (i.e., acidic) soils transition to neutral pH (i.e., pH≈7 ), dissolved CO2 is converted to the alkaline dissolved mineral bicarbonate (HCO3−). Near PH=7 bicarbonate is the dominant form of DIC. In other words, based on the shifting of the pH value, CO2 is converted to HCO3− and is not released as gas into the atmosphere.\|[0025] Next it is investigated what happens after CO2 is converted to other forms of dissolved inorganic carbon. After the conversion from CO2 to HCO3−, the bicarbonate (HCO3−) percolates into streams and rivers, from where the bicarbonate is delivered to the oceans. This DIC may reside in groundwater within the soil column for decades to centuries. This is an effective removal of carbon dioxide available to the ocean-atmosphere system. The eventual precipitation of bicarbonate as calcium carbonate minerals in deep aquifers or after transport to the ocean stably stores carbon for more than 10,000 years. The delivery of DIC to the ocean in the form of bicarbonate acts to enhance ocean alkalinity, which is vital for the health of ocean flora and fauna. For example, coral ecosystems have been particularly damaged by ocean acidification which is a well-known side effect of climate change. Ocean alkalinity enhancement works to counteract ocean acidification, as shown in 110 of FIG. 1A.\|Technical Problems\|[0026] It is hard to measure carbon capture. In agricultural and forest environments, many methods have been developed for measuring how much carbon is stored in soil. These methods significantly rely on labor-intensive mass-spectrometer measurements, spectroscopy, satellite-based sensors, and modeling. However, understanding the ecosystematic changes in soils is complex, as conditions may vary across a single plot of land. These methods cannot accurately evaluate carbon captured and retained in soils. Most current projects/methods cannot successfully quantify the amount of carbon, much less report carbon sequestration and conservation confidently. These schemes do not help address or incentivize emission avoidance and reduction by high-carbon industries (including agriculture).\|[0027] Even if the issue of carbon measurement can be solved, there are other challenges such as carbon deception. This is another main challenge related to the “net zero” demand in ecosystems. “Net zero” refers to a situation where an amount of carbon dioxide is removed from the atmosphere after that amount of carbon dioxide emission is generated, resulting in zero increase in net emissions. Thus, gas emission is still generated from human activity (e.g., fossil fuel companies can continue to explore, drill, extract, and burn fossil fuels), but carbon dioxide is taken out of the atmosphere in certain ways in some other places to balance out emissions. However dishonest actors may present during this procedure. For example, like a manufacturer rigging vehicles to cheat on emissions tests, forestry interventions may cut trees and then replant trees to claim carbon gains, i.e., carbon deception. Monitoring, reporting, and verification (MRV) is the process that can account for, communicate, and certify a CDR system's carbon removal over time. Currently, ERW lacks a robust MRV framework to obtain proper knowability of carbon sequestration (e.g., detecting carbon deception) and fill the knowledge gap to fulfill the demand of “net zero.”\|[0028] MRV is technically difficult due to the long timescales and uncertainties associated with the chemical and physical processes involved. Some crucial issues in MRV include accurately tracking carbon uptake, ensuring the permanence of carbon storage (e.g., long-time leakage risk), dealing with the variability of the process across different conditions, developing standardized reporting methods that ensure credibility and comparability across projects, etc. For example, there is no feasible way to directly measure the amount of CO2 removed from the atmosphere by ERW, and measuring CO2 in soils and groundwater is inherently challenging due to variability in environmental conditions (e.g., temperature, moisture levels, soil type, microbial activity). Emerging technologies (e.g., remote sensing, advanced soil sampling techniques) and research on effective MRV may help overcome some of the challenges.\|Overview\|[0029] The present disclosure proposes a novel system and method for performing compositional characterization of soil-rock dust mixtures. In some embodiments, the present system includes laser induced breakdown spectroscopy (LIBS) instruments that embody new MRV methodologies for ERW. LIBS deduces the elemental composition of a sample (e.g., solids, liquids, and gases) from measurements of the spectral line emission emitted by the plasma produced by high-power laser irradiation of the sample. LIBS will be described in further detail below.\|[0030] In some embodiments, the proposed workflow as described herein may include four primary facets:\| - i. Choose where to sample and measure compositional characteristics of soils;\| - ii. Determine how to measure compositional characteristics of the soils using LIBS;\| - iii. Analyze LIBS measurements (e.g., based on existing gold-standard measurement techniques); and\| - iv. Use post-processing analytical tools to create high-quality, verifiable carbon credits (a tradable certificate used to reduce global greenhouse gas emissions).\|[0035] The present disclosure also proposes multiple LIBS devices that may be employed in the field, workstations, or laboratories.\|[0036] FIG. 2A illustrates an overview of an exemplary LIBS-based data system 200 that is used to implement the functionalities described herein. In this example, system 200 includes a sample handling unit 202, a LIBS device 204, and a data processing unit 206. System 200 may use sample handling unit 202 to identify locations or zones that target samples (e.g., soil samples) should be collected from (e.g., geolocated zone-based soil sampling). Depending on different quantitative analyses and qualitative analyses to be performed (e.g., as described in FIGS. 3-6), sample handling unit 202 may also be used to instruct LIBS device 204 to obtain specific types of measurements. The present system may further use sample handling unit 202 to ensure the accurate positioning of a sample for optical interaction with LIBS device 204. LIBS device 204 is employed to obtain measurements and analysis data from samples, which will be described in detail in FIG. 2B. The data from LIBS device 204 is further analyzed and modeled by data processing unit 206 for the purpose of monitoring, reporting, and verification, for example, as illustrated in FIG. 5 below. Although only one LIBS device is shown in the example system 200 of FIG. 2A, it is possible that more LIBS devices and/or other units/components may be included in a LIBS-based data system.\|[0037] In some embodiments, at least a portion of the data processing unit 206 is part of a computer system (described below in FIG. 7) that is communicatively coupled to LIBS device 204. In other embodiments, at least a portion of the data processing unit 206 may be integrated into LIBS device 204. For example, data processing unit 206 may reside on a standalone computer system to perform advanced compositional analysis based on real-time sample analysis from data acquisition & analysis component 260 of LIBS device 204 (described below in FIG. 2B). Data processing unit 206 together with data acquisition & analysis component 260 form a data analysis subsystem that is responsible for various types of data processing, evaluation, calculation, etc, as described in the present disclosure. When LIBS device 204 is attached to or mounted on a motor instrument (e.g., vehicle, drone), the data analysis subsystem may be integrated into data acquisition onboard the motor instrument for real-time data acquisition and analysis. In some embodiments, at least a portion of the sample handling unit 202 may also be part of an external computer system and/or an integrated part of LIBS device 204. For example, sample handling unit 202 may be designed to use motorized stages or robots to move a sample in a controlled manner and thus is included in or attached to LIBS device 204 for precise sample positioning.\|LIBS Device\|[0038] LIBS is a rapid chemical analysis technology that uses a short laser pulse to create a micro-plasma on the sample surface. LIBS can be used to detect the presence of various elements in a sample based on directing a high-power emission from a laser onto the sample to form a plasma. The plasma is then analyzed spectroscopically to determine the composition of the sample. The LIBS is often used with a soil penetrating probe to detect heavy metal contamination in soil due to its high sensitivity and sample-free preparation. The LIBS analytical technique offers some other compelling advantages such as fast measurement time (e.g., a few seconds for a single spot analysis), broad elemental coverage (e.g., including, but not limited to, lighter elements such as H, Be, Li, C, N, O, Na, and Mg), versatile sampling protocols that include fast raster of the sample surface and depth profiling, etc.\|[0039] The present disclosure proposes new LIBS device(s) used in the MRV process for ERW. In some embodiments, the new LIBS device is a single multi-purpose optical device. In other embodiments, the new LIBS device may include one or more optical devices. Each device can be designed for a single purpose or multiple purposes. The LIBS devices may have various physical components and/or configurations.\|[0040] FIG. 2B illustrates an overall block diagram of an exemplary LIBS device 204, which includes some key components such as optical source 254, focusing and light collection optics 256, detector 258, and data acquisition & analysis component 260. These components are depicted merely for illustration, and other components (more or less) may be included in LIBS device 204. For example, sample probe 252 may be part of the LIBS device 204. In some embodiments, LIBS device 204 may use a sample probe 252 (e.g., a soil penetrating probe) to take a sample from a target area that is strategically identified (e.g., on managed land). In response, optical source 254 (e.g., a laser) may generate a high-energy light pulse that is directed onto the sample, and focusing and light collection optics 256 (e.g., lens, mirrors) may focus the light pulse to a specific point on the sample, thereby creating a plasma plume. The focusing and light collection optics 256 may also capture/collect the light pulse/beam to avoid light interference. The collected light pulse is then passed through detector 258 (e.g., spectrometer) to obtain sample measurements (e.g., spectral data). For example, detector 258 may disperse the light pulse into individual wavelengths, determine the intensity of light at each wavelength (e.g., using a charge-coupled device (CCD) or photo-multiplier tube (PMT)), and generate a spectrum that is characteristic of specific elements in the sample.\|[0041] Data acquisition & analysis component 260 may include computing hardware such as a central processing unit, memory, and storage, as described in the computer system of FIG. 7. Data acquisition & analysis component 260 is configured to receive the measurement data from detector 258 and perform the elemental composition analysis on the measurement data. In some embodiments, LIBS device 204 may also communicate with an alternative or additional data processing unit (e.g., 206) to perform LIBS analysis and any other elemental identification and quantification analyses. Based on the analysis, a result is generated in 262. For example, the result may be a report or graphical output showing the elemental composition of the sample. Various types of measurements and analyses may be conducted by the data analysis subsystem including data acquisition & analysis component 260 and data processing unit 206, which will be further described below with reference to FIGS. 3-6.\|[0042] The present system may deploy one or more improved LIBS devices to implement the disclosed functionalities. For example, the improved LIBS device (e.g., 204) may be equipped, attached, or associated with an autofocusing component to enable consistent, in-focus measurements of samples without moving other optical components. The autofocusing component may be included as a part of a suitable optical assembly that is hand-held, attached to a mobile vehicle, or integrated with a positioning system (e.g., robotic arm, boom, leg, conveyor belt), etc. Using the autofocusing component, spectroscopy measurements can be automatically focused based on a focal length of its optics relative to the target sample. Instead of using certain mechanisms (e.g., mechanical actuators) to change the position of the optical component(s), in some embodiments, the autofocusing component may include a shape changing lens (e.g., variable focus lens) to allow continuous tuning of a focal length and working distance of the autofocusing component relative to a target sample.\|Data Acquisition and Evaluation Using LIBS Device\|[0043] As discussed above, components 252, 254, 256, 258, and/or 260 of LIBS device 204 may work together with other units of data system 200 to acquire sample data and provide insights about the elemental composition of a sample (e.g., soil sample). In the illustrated embodiment of FIG. 3, one or more LIBS devices 204 may be used to determine weathering status 304, evaluate specific soil contents/elements 306, calculate heavy metal concentration 308, evaluate metal ratios in soils 310, and/or measure soil organic carbon 312. In some embodiments, one or more LIBS devices 200 may also be used to measure and analyze the compositional characteristics of soils, the biological composition of plant and seed matter, and the elemental composition of rock samples.\|[0044] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) used for determining weathering status 304. In some embodiments, a LIBS-based device may be employed to assess the composition of lighter cations relative to heavier cations in applied rock dust. This composition analysis may be used in determining the weathering status of the rock dust application on agricultural fields, pasture lands, or any other natural environments. Thus, an approach is obtained, for determining the loss of rock dust due to enhanced rock weathering (ERW) for the purpose of monitoring, reporting, and verification (MRV) to create carbon credits.\|[0045] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating specific soil elements 306, for example, the nitrogen (N), phosphorus (P), and potassium (K) content of the soil. This is the estimation of nutrient requirements, factoring in additional nutrients provided by rock dust application. The use of LIBS devices in elemental composition analysis can reduce farmers' burden to apply fertilizers (i.e., NPK nitrogen-phosphorus-potassium) while conducting ERW projects. LIBS allows the quantification of these additional bioavailable nutrients, which become active in the soil column with the breakdown of the rock minerals (e.g., being modified through chemical, physical, or biological interactions with rocks and minerals).\|[0046] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for calculating heavy metal concentrations 308, e.g., the amounts of metallic elements (often toxic) found in the soils or rock dust used for ERW. These elements may include metals such as lead (Pb), mercury (Hg), nickel (ni), etc., and can be found in pesticides, fertilizers, or untreated sewage sludge introduced into the soil. The heavy metal may accumulate in the environment to pose serious health and ecological risks. The disclosed LIBS device may provide insights into the safety considerations of cultivating various crops, for example, providing insights into phytoremediation such as using sunflowers to remove Strontium, which is poisonous metal to most other livings. According to US Environmental Protection Agency (EPA) standards, the bio-availability of metals and dissolved aqueous metals will be needed for calculating heavy metal concentrations.\|[0047] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating key metal ratios in soils for ERW 310. In some embodiments, critical metal ratios in soils are assessed using LIBS technology before the implementation of ERW (i.e., before the rock dust application for enhanced weathering). This process can be outlined as follows:\| - i. Sample Collection: soil samples are collected from the target area where ERW is planned. These samples represent the current soil composition in the region;\| - ii. LIBS Analysis: the collected soil samples are subjected to LIBS analysis. The LIBS device measures the elemental composition of the soil, providing baseline data on the concentrations of various metals being present;\| - iii. Trace metal ratios and potential pulverized rock dust field amendments may then be evaluated together to determine if the rock dust is appropriate for application to the field; and \| - a. Evaluate environmental concerns,\| - b. Evaluate the potential for signal strength in measurements: measuring key metal ratios for MRV process.\| - iv. Key Metal Ratios: specific metal ratios of interest, which are known to influence the effectiveness of ERW, are calculated based on the LIBS data. These key metal ratios often include ratios such as calcium to magnesium (Ca/Mg), calcium to potassium (Ca/K), or calcium to sodium (Ca/Na), among others.\|[0054] In some embodiments, the calculated key metal ratios are evaluated to determine the suitability of the soil for ERW. An ideal balance of these ratios is typically necessary for optimal carbon capture and weathering outcomes. The assessment results may guide decisions regarding the need for rock dust application and the specific rock dust type required to achieve the desired metal ratios for effective ERW.\|[0055] By employing LIBS technology for the evaluation of key metal ratios in soils before rock dust application for enhanced weathering, informed decision-making can be used to ensure that the chosen ERW strategy is tailored to the specific soil composition of the target area. This optimization may also contribute to efficient carbon dioxide removal and MRV.\|[0056] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for measuring soil organic carbon 312. A LIBS device can be used to measure soil organic carbon (SOC) levels. The SOC level represents the amount of carbon stored in the form of organic compounds in the soil, and SOC is critical to soil quality and carbon sequestration because it helps store carbon from the atmosphere and contributes to mitigating climate change. By measuring the SOC level, the present disclosure facilitates the correlation between changes in organic carbon attributable to rock dust application, thereby offering valuable insights into soil improvement. In some embodiments, soil organic carbon measurements may be approximated by the loss of material on ignition (LOI) (e.g., by measuring the weight loss of organic matter content after heating the sample to a high temperature).\|LIBS Analysis\|[0057] Numerous LIBS analyses may be conducted based on element measurements, calculation, and evaluation. In addition to in-depth soil analysis, when a LIBS device is used to measure the biological composition of plant and seed matter, the LIBS analysis can serve to validate the absence of potential metal accumulation resulting from enhanced weathering processes.\|[0058] In some embodiments, a LIBS device may also be used for rock sample analysis, where the elemental composition of raw rock samples from rock quarries or in the field is analyzed. This LIBS analysis may be applied to determine an enhanced weathering potential and a total carbon dioxide removal (CDR) potential. The enhanced weathering potential is the amount of atmospheric carbon dioxide that can be removed and stored through the ERW process (e.g., manual application of rocks or minerals) over a specific period of time. This factor may vary depending on the type of rocks/minerals used in ERW, the surface area available for reaction, environmental conditions (e.g., precipitation, temperature), etc. The total CDR potential is the amount of carbon dioxide that can be removed from the atmosphere in the long term, which depends on the effectiveness of the ERW process.\|[0059] In some embodiments, a spectral fluorescence device may be used in combination with LIBS analysis to create a dual system. This dual system enables the simultaneous determination of organic carbon and elemental composition in samples. This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status. In some embodiments, this approach may also be used to help refine soil organic carbon estimates outlined in 312 of FIG. 3. In general, the combination of LIBS and fluorescence may expand and strengthen the LIBS measurement and analysis, e.g., as discussed in FIG. 3.\|Beneficial Features of LIBS Device and Analysis\|[0060] FIG. 4 illustrates a block diagram 400 of exemplary features of LIBS devices and analysis used in the MRV process for ERW as described in the present system.\|[0061] The present system allows improved statistical accuracy with pooled/composite soil samples, as shown in 402. By aggregating soil samples from various locations within a field, the present system seeks to accurately determine the central compositional tendency and associated dispersion or variance in the soil's elemental composition. As compared to the current techniques, the utilization of pooled samples enables a more robust and representative analysis of the soil's overall composition, contributing to a more precise assessment of soil quality and environmental conditions. The accurate measurement of pooled samples is particularly important to soil fertility assessment, soil quality monitoring, and precision agriculture.\|[0062] The present system provides geolocated zone-based soil sampling for target characteristic assessment, as shown in 404. In some embodiments, the present system allows the collection of soil samples from specific geolocated zones within a field. By strategically pooling samples from these distinct zones, the analysis can yield precise data regarding the central tendency and variance of the target characteristic within each zone. This geolocated zone-based sampling approach offers a granular understanding of the spatial heterogeneity, distribution, and variability of the target characteristic, thereby enabling informed decision-making for soil management and ERW applications. Potential future obstacles with a MRV process based on soil heterogeneity may also be addressed by examining measurements at this juncture. In some embodiments, zones may be determined based on soil type, gridded areas, etc. A zone may also be small, predefined regions that include, but are not limited to, a circular region with a predefined radius or a square area with a predefined side length.\|[0063] The LIBS device of the present system can be used in rock sample analysis to determine enhanced weathering potential and total carbon dioxide removal (CDR) potential. In particular, the present system may evaluate the carbon dioxide potential of alkaline silicate minerals, as shown in 406. The present system can assess the carbon dioxide potential of alkaline silicate minerals including, but not limited to, basalt, olivine, and wollastonite. These minerals are known for their capacity to sequester carbon dioxide through enhanced weathering processes. In some embodiments, the present system may utilize a LIBS device to analyze the elemental composition of these minerals and determine their specific potential for CDR. By accurately quantifying the CDR potential of alkaline silicate minerals, the present system gains valuable insights into the efficacy of a CDR solution.\|[0064] The present system allows systematic preparation of pressed-pelletized subsamples derived from pooled soil samples, as shown in 408. By compressing and pelletizing soil material from each pooled sample, the present system may create a consistent and standardized substrate for LIBS analysis. This process can minimize variations in sample presentation, ensuring reliable and reproducible results during LIBS analysis. This process further streamlines the handling of samples, allowing for an efficient assessment of the central compositional tendency and variance of the target characteristics within the soil, and ultimately enhancing the accuracy of soil quality and environmental assessments.\|[0065] The present system further allows grid-based or rastered LIBS sampling for in-depth soil core analysis, as shown in 410. In some embodiments, the present system may conduct grid-based or rastered analyses of the pelletized subsamples, where the LIBS device systematically scans and analyzes discrete regions or points on the pellet surface in a structured grid or raster pattern. This approach enables a comprehensive examination of the intersample heterogeneity (or microheterogeneity) of soil characteristics and the distribution of elemental composition within the subsamples.\|[0066] Through this analysis, the present system may achieve a high-resolution understanding of the central compositional tendency and variance of the target characteristics in the soil, and the detailed information may provide invaluable insights into the spatial variability of soil properties, thereby enhancing precision in soil quality assessment and MRV for CDR applications.\|[0067] Using rasterized or gridded LIBS sampling can also systematically measure the elemental composition of intact soil cores at various depths. By taking measurements in a prescribed structured grid or raster pattern for LIBS analysis along the length of an intact soil core, the present approach enables precise characterization of the compositional variations with depth. This is particularly beneficial for understanding how soil properties change at different depths within the core, offering crucial insights into subsurface composition and environmental conditions. The present system seeks to assess soil heterogeneity and geological attributes with depth, contributing to informed decisions in ERW applications and MRV techniques.\|Device Characteristics and Deployment\|[0068] The present system supports specific device characteristics and deployment that are beneficial to the MRV process for ERW. In some embodiments, the present system supports handheld and miniaturized LIBS devices for soil sampling, field-based depth-integrated soil profiling with LIBS and soil auger, and in-field deployment of LIBS technology on motor vehicles, etc.\|[0069] The LIBS device described herein can be a handheld device that is portable, easy to operate, and suitable for rapid data acquisition. This handheld device is particularly useful in patchwork small-holder farms (e.g., rice paddies). It is engineered to provide a simplified user interface while maintaining the analytical accuracy and precision required for soil and environmental analysis. Any instantiation of the LIBS device may contain fewer optical sensors than the original, making the device more affordable and lighter. As a result, this LIBS device is adaptive for use in rural, remote, and economically disadvantaged communities. In addition, the miniaturized form of the device enables the present system to perform real-time, in-situ analyses, contributing to timelier and data-driven decision-making processes in agriculture, geology, and environmental science.\|[0070] The present system also allows a LIBS device to be combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic. A soil auger is employed to collect soil samples at various depths within the field. These samples are representative of the soil composition at specific depth intervals.\|[0071] After and/or during the auguring process, the present system performs LIBS analysis on the collected soil samples. A LIBS device can rapidly and accurately measure the elemental composition of the soil samples, including the concentration of the target characteristic of interest. The present system may then integrate the LIBS data obtained from each depth interval to construct a depth-integrated soil profile of the target characteristic. This profile provides a comprehensive understanding of how the target characteristic varies with depth within the soil.\|[0072] A LIBS device/instrument can be deployed in different ways. In some embodiments, the present system supports in-field deployment of LIBS technology on motor vehicles. LIBS is integrated into motor vehicles, such as tractors or other agricultural machinery, for in-field deployment. The present system seamlessly integrates LIBS instrumentation into the design of motor vehicles used for field operations, such as tractors.\|[0073] The LIBS device can be securely mounted, ensuring stability during vehicle movement. The LIBS device may operate in real time as the motor vehicle traverses the field. The LIBS device continuously analyzes the soil or other target materials as the vehicle moves, providing instant elemental composition data. The present system may collect LIBS-generated data and integrate the data into a data acquisition (DAQ) onboard the vehicle, allowing for real-time decision-making based on soil or material composition. A vehicle operator can use the LIBS data to make immediate adjustments to field operations for any ERW-related purpose, such as varying fertilizer application rates or adjusting rock dust application rates based on the in-field analysis. The present system may log the LIBS data, providing a detailed record of the soil or material composition across the field for subsequent analysis and optimization.\|[0074] In some embodiments, the present system may support other deployment methods. For example, one or more LIBS devices may be integrated into drones, underwater vehicles/amphibious, or other mobil instruments.\|Data Analysis and Modeling\|[0075] FIG. 5 illustrates a block diagram 500 of exemplary features of data analysis and modeling used in the present system. As depicted in FIG. 5, the data analysis and modeling 502 of the present system may be featured with various analytical tools such as multivariate distribution modeling for cation covariance analysis 504, empirical modeling for weathering prediction and carbon credit creation 506, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data 508, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS 510, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV 512. In some embodiments, these data analyses and modeling may be performed at least by data processing unit 206 in combination with data acquisition & analysis component 260 as shown in FIGS. 2A and 2B (i.e., data analysis subsystem).\|[0076] The present system provides multivariate distribution modeling for cation covariance analysis, as shown in 504. In some embodiments, the LIBS data can be leveraged for analyzing and modeling the covariance relationships among key cations in soil including, but not limited to, titanium, calcium, sodium, magnesium, potassium, phosphorous, and nitrogen. In some embodiments, the present system entails fitting multivariate normal or non-normal distributions to the data obtained through LIBS measurements.\|[0077] Multivariate distribution fitting allows for the comprehensive assessment of the covariance and correlations between key cations in soil. It provides valuable insights into the simultaneous variations and relationships among these elements, contributing to a deep understanding of soil composition and baseline information required for MRV. The present system uses LIBS to provide dense and rapid enough data to find systematic variances in soil heterogeneity within any given field, pasture, agricultural setting, or any other natural setting.\|[0078] In some embodiments, the present system may apply the quantitative elemental analysis approach as described in Sobron, titled “non-linear methods for quantitative elemental analysis and mineral classification using laser-induced breakdown spectroscopy (LIBS),” U.S. patent application Ser. No. 15/998,391, which is hereby incorporated by reference in its entirety.\|[0079] In some embodiments, the present system supports empirical modeling for weathering prediction and carbon credit creation, as shown in 406. That is, data collected in the present system can be leveraged to develop an empirically driven model for predicting the weathering of rock dust applied to fields and providing suggestions and instructions for subsequent ERW implementation.\|[0080] The empirical model may help the monitoring, reporting, and verification (MRV) process, which aims at quantifying the carbon capture potential resulting from enhanced weathering practices. By using dense, LIBS-generated data to create a predictive model, it becomes possible to monitor and report on the efficiency of carbon capture using regression-based and/or machine-learning methods. As a result, the time between data collection and sales for creating carbon credits may be reduced. The empirically driven model therefore facilitates accurate and data-driven MRV processes while incentivizing an easy switch to practices where carbon credits may be created through ERW. For example, when structure a predictive model, the present system may use mineral type, application rate, surface area of mineral, climate data, and environmental carbon dioxide concentration as input parameters of the model. The present system may calculate the weathering rate based on the environmental conditions and mineral properties, calculate the sequestration of carbon dioxide, and use weathering rate equations to predict how much carbon dioxide may be captured within a specific area over a specific timeframe. The present system may also calculate the total carbon dioxide removal rate to estimate global or regional carbon dioxide sequestration potential.\|[0081] To ensure accuracy and precision, in some embodiments, the present system may calibrate the LIBS device using high-precision measurements obtained from ICP-MS, as shown in 508.\|[0082] ICP-MS represents a well-established and highly accurate analytical technique, known for its exceptional precision in measuring elemental composition. By calibrating the LIBS device against ICP-MS data, the present system may establish a robust and reliable calibration framework. This calibration method may serve to validate and fine-tune the LIBS measurements, ensuring accuracy and traceability to a gold standard in elemental analysis.\|[0083] The integration of ICP-MS calibration in the present system enhances the trustworthiness and consistency of LIBS measurements, and the enhanced measurements may be suitable for a wide range of ERW applications for MRV. This calibration approach boosts the credibility of LIBS technology in scientific research and regulatory compliance (e.g., metals contamination according to EPA standards).\|[0084] The present system supports the construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, as shown in 510. In some embodiments, the present system may use known mixtures of soil and rock dust to create calibration curves. With a soil sample and rock dust sample that have already been characterized via ICP-MS or other analytical techniques, the present system can obtain known mixtures such that the rock dust comprises a known percentage of the weight of a newly created sample. By testing many mixed samples using LIBS with an array of rock dust ranging from 0 to 100% weight by mass, the present system can determine a series of calibration curves. These curves may fit the compositional characteristics of a particular soil type-rock dust combination. The present system may then store the data for soil type-rock dust combinations, creating a large database of possible LIBS spectral signals for a range of possible compositional arrays. With a sufficiently large database, the present system can apply one or more regression-based, machine-learning-based tools, and principal component analysis to select the most optimal calibration curve for new measurement(s).\|[0085] Here, the present system aims to strengthen the credibility of carbon credit generation. In some embodiments, the present system may use the misfit of measurements to known calibration curves to quantify measurement uncertainty, so that carbon credit sales effectively incorporate potential variations in carbon capture into pricing structures.\|[0086] In some embodiments, the present system supports collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV, as shown in 512. In other words, ICP-MS and LIBS are used collaboratively to spot-check and validate the empirically driven model developed for CDR MRV. This process ensures that the model accurately reflects the carbon capture and sequestration processes in real-world applications, enhancing the reliability of carbon credit generation. The present system may also use the same collaborative framework to generate uncertainty models when upscaling the sample area for MRV. To upscale the sample area for MRV, test plots are used to make projections for larger fields, and/or several fields are used to project CDR for a region, etc. By systematically assessing variations and uncertainties using ICP-MS and LIBS data, these models provide insights into the potential variability in carbon capture estimates as the sample area is expanded. This information is essential for accurately quantifying carbon credits and assuaging buyers' concerns about the quality of carbon credits. The information is also crucial to assess the quality of MRV.\|[0087] The present system aims to strengthen the credibility of carbon credit generation and improve informed decision-making in ERW-related land management. By integrating uncertainty modeling, the present system enhances its ability to account for variations in carbon capture and carbon dioxide removal potential and provides a comprehensive assessment of carbon dioxide removal efforts. The present system may enhance the credibility of carbon credit generation while providing transparency and accountability in environmental initiatives.\|Flowchart\|[0088] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments. Method 600 may be implemented using a LIBS-based data system 200, as shown in FIGS. 2A and 2B. A spectroscopy device (e.g., LIBS device 204) is used to obtain measurements from a target sample. At step 602, the spectroscopy device (e.g., using optical source 254) emits one or more optical signals directed to a target collected from a target area (e.g., managed field or other agricultural settings). At step 604, the spectroscopy device (e.g., using detector 258) determines spectral measurements of the optical signals collected from the target. The target can be a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified (e.g., by sample handing unit 202) from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered LIBS sampling.\|[0089] As shown in FIGS. 2A and 2B, a data analysis subsystem (e.g., including data processing unit 206 and data acquisition & analysis component 260) is communicatively coupled to the spectroscopy device (e.g., LIBS device 204). At step 606, the data analysis subsystem is configured to convert the spectral measurements to data indicating compositional characteristics of the target, which includes at least one or more of determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. For example, to determine the weathering status, loss of rock dust may be determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering.\|[0090] The data analysis subsystem is then configured to analyze the data indicating compositional characteristics of the target using a plurality of analytical tools at step 608, and provide assessment on carbon dioxide removal and insights on enhanced rock weathering at step 610. In some embodiments, to analyze the compositional data, the data analysis subsystem uses various analytical tools to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision ICP-MS data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS, etc. To provide the assessment, the data analysis subsystem may also calculate one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.\|Computer Implementation\|[0091] In some examples, some or all of the processing described above can be carried out on a personal computing device, on one or more centralized computing devices, or via cloud-based processing by one or more servers. Some types of processing can occur on one device and other types of processing can occur on another device. Some or all of the data described above can be stored on a personal computing device, in data storage hosted on one or more centralized computing devices, and/or via cloud-based storage. Some data can be stored in one location and other data can be stored in another location. In some examples, quantum computing can be used, and/or functional programming languages can be used. Electrical memory, such as flash-based memory, can be used.\|[0092] FIG. 7 is a block diagram of an example computer system 700 that may be used in implementing the technology described herein. General-purpose computers, network appliances, mobile devices, or other electronic systems may also include at least portions of the system 700. The system 700 includes a processor 710, a memory 720, a storage device 730, and an input/output device 740. Each of the components 710, 720, 730, and 740 may be interconnected, for example, using a system bus 750. The processor 710 is capable of processing instructions for execution within the system 700. In some implementations, the processor 710 is single-threaded. In some implementations, the processor 710 is a multi-threaded processor. The processor 710 is capable of processing instructions stored in the memory 720 or on the storage device 730.\|[0093] Memory 720 stores information within the system 700. In some implementations, the memory 720 is a non-transitory computer-readable medium. In some implementations, the memory 720 is a volatile memory unit. In some implementations, the memory 720 is a non-volatile memory unit.\|[0094] The storage device 730 is capable of providing mass storage for the system 700. In some implementations, the storage device 730 is a non-transitory computer-readable medium. In various implementations, the storage device 730 may include, for example, a hard disk device, an optical disk device, a solid-state drive, a flash drive, or some other large-capacity storage device. For example, the storage device may store long-term data (e.g., database data, file system data, etc.). The input/output device 740 provides input/output operations for the system 700. In some implementations, the input/output device 740 may include one or more network interface devices, e.g., an Ethernet card, a serial communication device, e.g., an RS-232 port, and/or a wireless interface device, e.g., an 802.11 card, a 3G wireless modem, or a 4G wireless modem. In some implementations, the input/output device may include driver devices configured to receive input data and send output data to other input/output devices, e.g., keyboard, printer, and display devices 760. In some examples, mobile computing devices, mobile communication devices, and other devices may be used.\|[0095] In some implementations, at least a portion of the approaches described above may be realized by instructions that upon execution cause one or more processing devices to carry out the processes and functions described above. Such instructions may include, for example, interpreted instructions such as script instructions, executable code, or other instructions stored in a non-transitory computer-readable medium. The storage device 730 may be implemented in a distributed way over a network, such as a server farm or a set of widely distributed servers, or may be implemented in a single computing device.\|[0096] Although an example processing system has been described in FIG. 7, embodiments of the subject matter, functional operations, and processes described in this specification can be implemented in other types of digital electronic circuitry, in tangibly embodied computer software or firmware, in computer hardware, including the structures disclosed in this specification and their structural equivalents, or in combinations of one or more of them. Embodiments of the subject matter described in this specification can be implemented as one or more computer programs, i.e., one or more modules of computer program instructions encoded on a tangible nonvolatile program carrier for execution by, or to control the operation of, data processing apparatus. Alternatively or in addition, the program instructions can be encoded on an artificially generated propagated signal, e.g., a machine-generated electrical, optical, or electromagnetic signal that is generated to encode information for transmission to a suitable receiver apparatus for execution by a data processing apparatus. The computer storage medium can be a machine-readable storage device, a machine-readable storage substrate, a random or serial access memory device, or a combination of one or more of them.\|[0097] The term “system” may encompass all kinds of apparatus, devices, and machines for processing data, including by way of example a programmable processor, a computer, or multiple processors or computers. A processing system may include special-purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit). A processing system may include, in addition to hardware, code that creates an execution environment for the computer program in question, e.g., code that constitutes processor firmware, a protocol stack, a database management system, an operating system, or a combination of one or more of them.\|[0098] A computer program (which may also be referred to or described as a program, software, a software application, a module, a software module, a script, or code) can be written in any form of programming language, including compiled or interpreted languages, or declarative or procedural languages, and it can be deployed in any form, including as a standalone program or as a module, component, subroutine, or other unit suitable for use in a computing environment. A computer program may, but need not, correspond to a file in a file system. A program can be stored in a portion of a file that holds other programs or data (e.g., one or more scripts stored in a markup language document), in a single file dedicated to the program in question, or in multiple coordinated files (e.g., files that store one or more modules, sub programs, or portions of code). A computer program can be deployed to be executed on one computer or on multiple computers that are located at one site or distributed across multiple sites and interconnected by a communication network.\|[0099] The processes and logic flows described in this specification can be performed by one or more programmable computers executing one or more computer programs to perform functions by operating on input data and generating output. The processes and logic flows can also be performed by, and apparatus can also be implemented as, special purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit).\|[0100] Computers suitable for the execution of a computer program can include, by way of example, general or special purpose microprocessors or both, or any other kind of central processing unit. Generally, a central processing unit will receive instructions and data from a read-only memory, a random access memory, or both. A computer generally includes a central processing unit for performing or executing instructions and one or more memory devices for storing instructions and data. Generally, a computer will also include, or be operatively coupled to receive data from or transfer data to, or both, one or more mass storage devices for storing data, e.g., magnetic, magneto-optical disks, or optical disks. However, a computer need not have such devices. Moreover, a computer can be embedded in another device, e.g., a mobile telephone, a personal digital assistant (PDA), a mobile audio or video player, a game console, a Global Positioning System (GPS) receiver, or a portable storage device (e.g., a universal serial bus (USB) flash drive), to name just a few.\|[0101] Computer-readable media suitable for storing computer program instructions and data include all forms of non-volatile memory, media, and memory devices, including by way of example semiconductor memory devices, e.g., EPROM, EEPROM, and flash memory devices; magnetic disks, e.g., internal hard disks or removable disks; magneto-optical disks; and CD-ROM and DVD-ROM disks. The processor and the memory can be supplemented by, or incorporated in special-purpose logic circuitry.\|[0102] To provide for interaction with a user, embodiments of the subject matter described in this specification can be implemented on a computer having a display device, e.g., a CRT (cathode ray tube) or LCD (liquid crystal display) monitor, for displaying information to the user and a keyboard and a pointing device, e.g., a mouse or a trackball, by which the user can provide input to the computer. Other kinds of devices can be used to provide for interaction with a user as well; for example, feedback provided to the user can be any form of sensory feedback, e.g., visual feedback, auditory feedback, or tactile feedback; and input from the user can be received in any form, including acoustic, speech, or tactile input. In addition, a computer can interact with a user by sending documents to and receiving documents from a device that is used by the user; for example, by sending web pages to a web browser on a user's user device in response to requests received from the web browser.\|[0103] Embodiments of the subject matter described in this specification can be implemented in a computing system that includes a back-end component, e.g., as a data server, or that includes a middleware component, e.g., an application server, or that includes a front-end component, e.g., a client computer having a graphical user interface or a Web browser through which a user can interact with an implementation of the subject matter described in this specification, or any combination of one or more such back end, middleware, or front end components. The components of the system can be interconnected by any form or medium of digital data communication, e.g., a communication network. Examples of communication networks include a local area network (“LAN”) and a wide area network (“WAN”), e.g., the Internet.\|[0104] The computing system can include clients and servers. A client and server are generally remote from each other and typically interact through a communication network. The relationship between client and server arises by virtue of computer programs running on the respective computers and having a client-server relationship with each other.\|[0105] While this specification contains many specific implementation details, these should not be construed as limitations on the scope of what may be claimed, but rather as descriptions of features that may be specific to particular embodiments. Certain features that are described in this specification in the context of separate embodiments can also be implemented in combination in a single embodiment. Conversely, various features that are described in the context of a single embodiment can also be implemented in multiple embodiments separately or in any suitable sub-combination. Moreover, although features may be described above as acting in certain combinations and even initially claimed as such, one or more features from a claimed combination can in some cases be excised from the combination, and the claimed combination may be directed to a sub-combination or variation of a sub-combination.\|[0106] Similarly, while operations are depicted in the drawings in a particular order, this should not be understood as requiring that such operations be performed in the particular order shown or in sequential order, or that all illustrated operations be performed, to achieve desirable results. In certain circumstances, multitasking and parallel processing may be advantageous. Moreover, the separation of various system components in the embodiments described above should not be understood as requiring such separation in all embodiments, and it should be understood that the described program components and systems can generally be integrated together in a single software product or packaged into multiple software products.\|[0107] Particular embodiments of the subject matter have been described. Other embodiments are within the scope of the following claims. For example, the actions recited in the claims can be performed in a different order and still achieve desirable results. As one example, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In certain implementations, multitasking and parallel processing may be advantageous. Other steps or stages may be provided, or steps or stages may be eliminated, from the described processes. Accordingly, other implementations are within the scope of the following claims.\|Terminology\|[0108] The phraseology and terminology used herein are for the purpose of description and should not be regarded as limiting.\|[0109] The term “approximately”, the phrase “approximately equal to”, and other similar phrases, as used in the specification and the claims (e.g., “X has a value of approximately Y” or “X is approximately equal to Y”), should be understood to mean that one value (X) is within a predetermined range of another value (Y). The predetermined range may be plus or minus 20%, 10%, 5%, 3%, 1%, 0.1%, or less than 0.1%, unless otherwise indicated.\|[0110] The indefinite articles “a” and “an,” as used in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.” The phrase “and/or,” as used in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Multiple elements listed with “and/or” should be construed in the same fashion, i.e., “one or more” of the elements so conjoined. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, a reference to “A and/or B”, when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A only (optionally including elements other than B); in another embodiment, to B only (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc.\|[0111] As used in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of,” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of,” “only one of,” or “exactly one of.” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law.\|[0112] As used in the specification and in the claims, the phrase “at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements. This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase “at least one” refers, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, “at least one of A and B” (or, equivalently, “at least one of A or B,” or, equivalently “at least one of A and/or B”) can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc.\|[0113] The use of “including,” “comprising,” “having,” “containing,” “involving,” and variations thereof, is meant to encompass the items listed thereafter and additional items.\|[0114] Use of ordinal terms such as “first,” “second,” “third,” etc., in the claims to modify a claim element does not by itself connote any priority, precedence, or order of one claim element over another or the temporal order in which acts of a method are performed. Ordinal terms are used merely as labels to distinguish one claim element having a certain name from another element having a same name (but for use of the ordinal term), to distinguish the claim elements.\|[0115] Each numerical value presented herein, for example, in a table, a chart, or a graph, is contemplated to represent a minimum value or a maximum value in a range for a corresponding parameter. Accordingly, when added to the claims, the numerical value provides express support for claiming the range, which may lie above or below the numerical value, in accordance with the teachings herein. Absent inclusion in the claims, each numerical value presented herein is not to be considered limiting in any regard.\|[0116] The terms and expressions employed herein are used as terms and expressions of description and not of limitation, and there is no intention, in the use of such terms and expressions, of excluding any equivalents of the features shown and described or portions thereof. In addition, having described certain embodiments of the invention, it will be apparent to those of ordinary skill in the art that other embodiments incorporating the concepts disclosed herein may be used without departing from the spirit and scope of the invention. The features and functions of the various embodiments may be arranged in various combinations and permutations, and all are considered to be within the scope of the disclosed invention. Accordingly, the described embodiments are to be considered in all respects as only illustrative and not restrictive. Furthermore, the configurations, materials, and dimensions described herein are intended as illustrative and in no way limiting. Similarly, although physical explanations have been provided for explanatory purposes, there is no intent to be bound by any particular theory or mechanism, or to limit the claims in accordance therewith.	Family Number\|(114579754)\|114579754\|Abstract\|(US20250164404 A1)\|A method and system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. In some embodiments, the method includes emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area. The method includes determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target. The method includes converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target. The method also includes analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools. The method further includes providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.\|Title\|(US20250164404 A1)\|System and method for enhanced rock weathering monitoring, reporting, and verification\|Advantages / Prev. Drawbacks\|(US20250164404 A1)\| (...) This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status.\|However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions.\|Independent Claims\|(US20250164404 A1)\| (...) A system for monitoring, reporting, and verification of enhanced rock weathering comprising: (...) provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\| (...) A method for monitoring, reporting, and verification of enhanced rock weathering comprising: (...) providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.\|	Analysis of biological materials	G01N-021/71/8\|G01N-033/24\|G01N-033/24/1\|G01N-033/245\|G01N-2201/0216\|G01N-2201/0221\|G01N-2201/06113\|G01N-2201/12746		G01N-021/71/8\|G01N-033/24\|G01N-033/24/1\|G01N-033/245\|G01N-2201/0216\|G01N-2201/0221\|G01N-2201/06113\|G01N-2201/12746	G01N-021/71\|G01N-033/24	G01N-021/71\|G01N-033/24										PENDING	(US20250164404)\|PENDING	ALIVE	(US20250164404)\|ALIVE	(US20250164404)\|LEGAL DETAILS FOR US20250164404\|Actual or expected expiration date=2044-11-20\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-11-20\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US18954208\|Application date=2024-11-20\|Standardized application number=2024US-18954208\|Event publication date=2024-11-20\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:DOUMBIA, MOHAMED\|Event publication date=2024-11-20\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: IMS-002US\|Event publication date=2024-11-20\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 162143\|Event publication date=2024-11-20\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2024-11-20\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2024-11-20\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=2877\|Event publication date=2024-11-20\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2024-11-20\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2024-11-20\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2024-11-26\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2024-11-29\|Event code=US/POAC\|Event group=Change of name or address\|Change in Power of Attorney (May Include Associate POA)\|Event publication date=2024-11-29\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2024-12-27\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2024-12-27\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-05-22\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250164404\|Publication stage code=A1\|Publication date=2025-05-22\|Standardized publication number=US20250164404\|Event publication date=2025-05-22\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2026-03-22\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner		(US20250164404)\|US	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcOL9D3zefy0h3ePXCJGwxO7JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022751788&ekey=2410&xpn=US20250164404&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/18954208/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=YH%252BWdJIGbNl11gTCkuP4xcRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(US20250164404)\|US	(US20250164404)\|NAME=Impossible Sensing LLC , CITY=St. Louis , STATE=MO , COUNTRY=US NAME=Mati Carbon PBC , CITY=Wilmington , STATE=DE , COUNTRY=US			(US20250164404)\|US; US; US	(US20250164404)\|NAME=Sobron Pablo, CITY=St. Louis, STATE=MO , COUNTRY=US \|NAME=Jordan Jacob S., CITY=St. Louis, STATE=MO , COUNTRY=US \|NAME=Agarwal Shantanu, CITY=Houston, STATE=TX , COUNTRY=US	(US20250164404)\|7	2	1					(US20250164404)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,14\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|	(US20250164404)\|Provisional Appl: US63/601,059 FDD=2023-11-20 [2023US-63601059]	(US20250164404)\|ENGLISH (ENG)	(US20250164404)\|Patent	Titre: (US20250164404)\|System and method for enhanced rock weathering monitoring, reporting, and verification Résumé: (US20250164404)\|A method and system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. In some embodiments, the method includes emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area. The method includes determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target. The method includes converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target. The method also includes analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools. The method further includes providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.	7	Abstract	gpt-4o-mini	yes	The article focuses on monitoring and verifying enhanced rock weathering, which is directly related to the process of accelerating mineral weathering for CO₂ removal.
5	AU2009900426\|AU2010210311\|WOAU2010/000124	WOAU2010/000124\|HK12105806\|IN6815/DELNP/2011\|EP10738163\|CN201080013080\|AU2010210311	IN6815/DELNP/2011\|HK1164777\|EP2393577\|CN102395417\|EP2393577\|AU2010210311\|WO2010/088738	1878278	WO2010/088738 A1 2010-08-12 [WO201088738]\|HK1164777 A 2012-09-28 [HK1164777]\|IN6815/DELNP/2011 A 2012-12-14 [IN2011DN06815]\|EP2393577 A4 2012-08-01 [EP2393577]\|EP2393577 A1 2011-12-14 [EP2393577]\|CN102395417 A 2012-03-28 [CN102395417]\|AU2010210311 A1 2011-09-01 [AU2010210311]	2009-02-06\|2010-02-08	2010-02-08\|2012-06-14\|2011-09-06\|2010-02-08\|2010-02-08\|2010-02-08	2012-12-14\|2012-09-28\|2012-08-01\|2012-03-28\|2011-12-14\|2011-09-01\|2010-08-12		(EP2393577)\|2014-09-02\|(WO2010/088738)\|2012-08-06\|(CN102395417)\|2014-12-03\|(IN6815/DELNP/2011)\|2022-12-14\|(HK1164777)\|2017-09-28\|(AU2010210311)\|2014-09-04	(EP2393577)\|System, apparatus and method for carbon dioxide sequestration	(EP2393577)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.	HUNWICK RICHARD J ([AU])\|Hunwick Richard J ([AU])\|HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD J. ([AU])\|HUNWICK RICHARD J ([AU])	(EP2393577)\|Hunwick, Richard J. ([AU])\|(EP2393577)\|Hunwick, Richard J. ([AU])\|(WO2010/088738)\|HUNWICK, Richard, J. ([AU])\|(CN102395417)\|HUNWICK RICHARD J. ([AU])\|(IN6815/DELNP/2011)\|HUNWICK RICHARD J ([AU])\|(HK1164777)\|Hunwick Richard J ([AU])\|(AU2010210311)\|Hunwick Richard	HUNWICK RICHARD J	(EP2393577)\|Hunwick, Richard J.\|(EP2393577)\|Hunwick, Richard J.	(EP2393577)\|De Clercq, Ann G. Y.;De Clercq & Partners ([BE])\|Reg. Nb: 101201288\|(WO2010/088738)\|GRIFFITH HACK ([AU])\|(CN102395417)\|LIU JIFU;CHINABLE INTELLECTUAL PROPERTY\|WANG LEI;CHINABLE INTELLECTUAL PROPERTY\|(HK1164777)\|MARKS & CLERK ([HK])\|(AU2010210311)\|Griffith Hack ([AU])	(WO2010/088738)\|A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor.\|It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations.\|The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage).\|However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\|If the quantities of calcium oxide naturally present in fly ash are inadequate, they may, in an embodiment, be augmented by adding pulverised limestone to raw power station flue gases in the boilers at one or more locations for example immediately upstream of the economiser section of the boilers, where flue gas temperatures are appropriate for the decomposition of limestone to calcium oxide and carbon dioxide (when exposed to furnace temperatures of 1,0000C or more, limestone is calcined to quicklime.\|The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s).\|	(WO2010/088738)\|1. A carbon dioxide sequestration process including the steps of:(i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium carbonate that is able to absorb the carbon dioxide, whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate;(ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|24. A system for sequestering carbon dioxide from a gas stream, the system comprising:(a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and(b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|38. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica.\|39. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|44. A method substantially as hereinbefore described with reference to the accompanying drawings.\|45. A system substantially as hereinbefore described with reference to the accompanying drawings.\|	(WO2010/088738)\|In accordance with a second aspect of the present invention there is provided a system for sequestering carbon dioxide from a gas stream, the system comprising: (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and\|Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\|hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica. In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|	(WO2010/088738)\|METHANEDIONE(100,69)\|SLURRY(100,37)\|PIPELINE(100,28)\|SILICATE SLURRY(100,14)\|METAL SILICATE SLURRY(100,13)\|METHANEDIONE SEQUESTRATION(100,11)\|FLOW PATH(100,9)\|GAS STREAM(100,8)\|SEQUESTRATION(100,7)\|CARBON SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|CARBON SEQUESTRATION(100,2)\|AMMONIUM 1 BICARBONATE METAL(100,1)\|BICARBONATE METAL(100,1)\|FLOW PATH PROVISION(100,1)\|REACTIVE AMMONIUM 1 BICARBONATE METAL(100,1)\|HARTSHORN(91,13)\|LIMESTONE PULVERIZATION(91,6)\|METHANEDIONE RICH FLUE GAS(90,2)\|METAL SILICATE(74,37)\|REACTION SLURRY(73,16)\|MAGNESIUM RICH SILICATE(65,8)\|PULVERIZED LIMESTONE INTRODUCTION(63,2)\|METAL CARBONATE(58,10)\|BICARBONATE(56,12)\|REACTOR(52,26)\|METAL SILICATE ROCK(51,3)\|CHESHUNT MIXTURE(48,46)\|REACTION ENHANCEMENT(45,5)\|HARTSHORN SOLUTION(42,3)\|RECOVERED CHESHUNT MIXTURE(40,6)\|MOLECULAR AMMONIA(36,14)\|ABSORBENT SLURRY(34,15)\|RAW FLUE GAS(31,8)\|CHESHUNT MIXTURE SOLUTION(28,10)\|ECONOMIZER SECTION(28,3)\|SILICATE(25,9)\|SEPARATION SYSTEM(24,3)\|THICKENING TANK(23,8)\|INSOLUBLE METAL CARBONATE SILICA(23,2)\|UNDERGROUND CHAMBER(20,8)\|RESIDUAL AMMONIA SCRUBBER(20,4)\|FLUE GAS STREAM(20,1)\|OLIVINE(18,6)\|CARBONATE METAL SILICATE SLURRY(18,3)\|FLUE GAS(17,36)\|RECOVERY SYSTEM(17,3)\|METHANEDIONE PERMANENT SEQUESTRATION(17,1)\|AQUEOUS PHASE(16,23)\|SOLUTION CIRCULATION(16,14)\|CHAMBER PRODUCT(16,2)\|FEEDER(16,2)\|ULTRABASIC MINERAL(16,2)\|MINERAL CARBONATION(15,3)\|PRODUCING CHAMBER(15,2)\|CHILLING PLANT(14,3)\|BICARBONATE NH4HCO(14,2)\|COOL AQUEOUS PHASE(14,2)\|COOLING SYSTEM(14,2)\|HUNTER VALLEY(14,2)\|INCOMING SILICATE SLURRY(14,2)\|INEVITABLE BYPRODUCT(14,2)\|INSOLUBLE MAGNESIA(14,2)\|METAL SILICATE SOLID(14,2)\|METHANEDIONE SINK(14,2)\|MIXED SOLUTION(14,2)\|CHILLED AMMONIATED SLURRY(14,1)\|SULFATE ION(13,5)\|CARBONATED SILICATE SLURRY(13,1)\|METHANEDIONE TONNE(13,1)\|SERPENTINE QUARRY SITE(13,1)\|COAL FIRED POWER STATION(12,6)\|INSOLUBLE CARBONATE(12,3)\|THRESHOLD LEVEL(12,3)\|HOT SILICATE SLURRY(12,2)\|PERMANENT EMPLACEMENT(12,2)\|ULTRAMAFIC MINERAL(12,2)\|THICKENING STAGE(11,3)\|METHANEDIONE CONTENT(11,2)\|BLACK COAL MWE(11,1)\|CARBONATED MINERAL FINAL EMPLACEMENT(11,1)\|CENT METHANEDIONE(11,1)\|SPARINGLY SOLUBLE HYDRATED SALT(11,1)\|AMMONIA LOSS(10,3)\|AMMONIA ABSORPTION CHILLER(10,2)\|FINAL PERMANENT REPOSITORY(10,2)\|FIRED ELECTRICITY GENERATION PLANT(10,2)\|CARBAMATE NH4COONH(10,1)\|CLARIFIED SUPERNATANT(10,1)\|CLARIFIER OVERFLOW(10,1)\|DEINKING ASH(10,1)\|ELECTRICITY GWH(10,1)\|FIN FAN COOLER(10,1)\|GASEOUS METHANEDIONE(10,1)\|INSTALLATION CIRCUMSTANCE(10,1)\|METHANEDIONE FAVOR FORMATION(10,1)\|MINERAL QUARRY SITE(10,1)\|MOLECULAR METHANEDIONE CO2(10,1)\|MULTISTAGE BARREL PUMP(10,1)\|PRESSURIZED METHANEDIONE(10,1)\|QUICKLIME GYPSUM(10,1)\|SERPENTINE MG3SI2O(10,1)\|STACKED SUBCHAMBER(10,1)\|STAGE THICKENER OVERFLOW(10,1)\|TALL SCRUBBING CHAMBER(10,1)\|CARBON DIOXIDE(9,3)\|STATIC HEAD(9,2)\|POWER STATION SITE(8,8)\|SOX(8,7)\|INSOLUBLE SOLID(8,4)\|AMMONIUM HYDROXIDE NH4OH(8,2)\|MINERAL MATTER(8,2)\|PUMPING ENERGY(8,2)\|RETURN PIPELINE(8,2)\|SOLUBLE SALT(8,2)\|SOLUBLE SUBSTANCE(8,2)\|AMMONIA RECOVERY VESSEL(8,1)\|AUSTRALIAN CONTEXT(8,1)\|CIRCULATING SOLUTION DELUGING SPRAY(8,1)\|DENSE SLURRY STREAM(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|INCOMING REACTIVE SLURRY(8,1)\|LIME CALCINATION(8,1)\|LJUNGSTROM ROTARY(8,1)\|MERCURY VAPOR(8,1)\|METHANEDIONE ABSORPTION CHAMBER(8,1)\|METHANEDIONE RICH GAS(8,1)\|MINERAL CARBONATE(8,1)\|PYROXENE MINERAL(8,1)\|PYROXENE SILICATE MINERAL(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|SCRUBBING VESSEL(8,1)\|SLURRY CIRCULATION(8,1)\|THICKENER BALANCE(8,1)\|FLUE GAS FILTER(7,3)\|REACTION CHAMBER(7,3)\|REACTION SOLUTION(7,3)\|ABSORB SURPLUS SENSIBLE HEAT(7,1)\|ALKALINE INDUSTRY RESIDUE(7,1)\|AMMONIA ABSORPTION CHAMBER(7,1)\|AMMONIA MILLION(7,1)\|BOOSTER PUMPING STATION(7,1)\|CHILLING CAPACITY(7,1)\|CIRCULATING SOLUTION ACIDITY(7,1)\|CONCENTRIC PIPE(7,1)\|EMPLACEMENT CONTENT(7,1)\|FINAL THICKENER TANK(7,1)\|FUEL COMBUSTION(7,1)\|GEHO PUMP(7,1)\|HOT SLURRY RISING(7,1)\|INORGANIC COMPONENT(7,1)\|ION EQUILIBRIUM(7,1)\|IRON DISULFIDE FES(7,1)\|KEY CARBONATION REACTION(7,1)\|MINE SITE(7,1)\|MINE VOID(7,1)\|MOLL CO2(7,1)\|NATURAL SILICATE(7,1)\|NONVOLATILE MERCURIC OXIDE(7,1)\|OXIDIZING ENVIRONMENT(7,1)\|PAPER RECYCLING RESIDUE COMBUSTION(7,1)\|PIPELINE REACTOR CHOICE(7,1)\|PRE METHANEDIONE(7,1)\|PRETREATMENT EXTENT(7,1)\|RAW SLURRY(7,1)\|RELEVANT GOVERNMENT(7,1)\|RESIDUAL STREAM CIRCULATION(7,1)\|SCRUBBING ZONE(7,1)\|SPRAY BANK(7,1)\|THICKENER SEPARATION(7,1)\|UNDERGROUND REACTOR PRODUCT(7,1)\|FILTER CAKE(6,5)\|ADJACENT FLOW PATH(6,2)\|FEED STREAM(6,2)\|FILTRATION MEDIUM(6,2)\|NILO2CO(6,2)\|PRECIPITATE(6,2)\|WOLLASTONITE(6,2)\|ABSORPTION ZONE(5,1)\|AMMONIATED SOLUTION(5,1)\|BICARBONATE ION(5,1)\|CARBONATION PRODUCT(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FILTER CLOTH(5,1)\|FINAL REACTION SLURRY(5,1)\|FLUE GAS DESULFURIZATION SCRUBBER(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|IMPURITY GAS(5,1)\|MAGNESIUM ION(5,1)\|METHANEDIONE RATIO(5,1)\|METHANEDIONE SOURCE(5,1)\|MINERAL TRANSPORT(5,1)\|NEXT THICKENER TANK(5,1)\|PIPE REACTOR(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|POWER STATION BOILER ECONOMIZER(5,1)\|POWERFUL OXIDIZING AGENT(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECOMBINATION REACTION(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|REQUISITE EXTENT(5,1)\|SALT DISSOLUTION(5,1)\|SALT HYDRATION(5,1)\|SCRUBBING SOLUTION(5,1)\|SESQUICARBONATE(5,1)\|SLURRY FEED(5,1)\|SOLUTION OFNH4HCO(5,1)\|STRATEGIC LOCATION(5,1)\|STREAM RETURN(5,1)\|SUBSTANCE DISSOLUTION(5,1)\|SULFUR CONTENT(5,1)\|SULFUR DIOXIDE SO2(5,1)\|COUNTER CURRENT DECANTATION(4,15)\|2NH4HCO(4,1)\|6NH4HCO(4,1)\|AGITATION(4,1)\|AIR PREHEATING(4,1)\|ALIGNED CHAMBER(4,1)\|AMMONIA RATIO(4,1)\|AMMONIA RICH NORMAL CARBONATE(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SOLUTION(4,1)\|ANNULUS(4,1)\|AQUEOUS PHASE CENT(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BIOMASS(4,1)\|CARBONATE RICH CHESHUNT MIXTURE(4,1)\|CASO4 2H2O(4,1)\|CHESHUNT MIXTURE SALT(4,1)\|CHILLED SOLUTION(4,1)\|CLEAR OVERFLOW SOLUTION(4,1)\|CONCENTRIC INNER(4,1)\|COOL GAS(4,1)\|COOLING WATER CIRCULATION(4,1)\|CRUSHING(4,1)\|DELUGE(4,1)\|DISCHARGE END(4,1)\|DOLOMITE(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|DRIVING MAGNESIUM(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|EXCESS AQUEOUS PHASE(4,1)\|FLY ASH SOLID(4,1)\|HEADER(4,1)\|HEAT CONSERVATION(4,1)\|HIGHLY EFFICIENT SCRUBBER(4,1)\|HYDROGEN ION CONCOMITANT FORMATION(4,1)\|INDICATIVE MASS BALANCE FIGURE(4,1)\|INORGANIC SOLID(4,1)\|INTERMEDIATE SALT(4,1)\|IRRADIATION(4,1)\|LIDDELL POWER STATION(4,1)\|LIMESTONE(4,1)\|LUMP PRODUCT(4,1)\|MAFIC ROCK(4,1)\|\|(CN102395417)\|CARBON DIOXIDE(100,143)\|SILICATE SLURRY(100,17)\|METAL SILICATE SLURRY(100,15)\|CARBON DIOXIDE SEQUESTRATION(100,14)\|GAS STREAM(100,10)\|CARBON SEQUESTRATION(100,8)\|FLUID CHANNEL(100,8)\|PIPELINE(100,7)\|FLUID PASSAGEWAY(100,5)\|CARBON SEQUESTRATION(100,3)\|PULVERIZED LIMESTONE(100,3)\|AMMONIUM BICARBONATE METAL(100,2)\|BICARBONATE METAL(100,2)\|SEQUESTERING CARBON DIOXIDE(100,2)\|REACTED AMMONIUM BICARBONATE METAL(100,1)\|SLURRY REACTION(100,1)\|METAL SILICATE ROCK(78,11)\|AMMONIUM BICARBONATE(77,27)\|REACTION SLURRY(77,16)\|DEPTH UNDERGROUND(69,1)\|REACTOR(65,32)\|METAL SILICATE(64,36)\|MAGNESIUM RICH SILICATE(59,8)\|METAL CARBONATE(57,14)\|AMMONIUM CARBONATE(56,50)\|PRETREATMENT EXTENT(52,1)\|AMMONIUM BICARBONATE SOLUTION(47,6)\|CARBON DIOXIDE CAPTURE(43,1)\|AMMONIUM CARBONATE SOLUTION(42,20)\|CARBONATE RICH SOLUTION(42,2)\|BICARBONATE(38,9)\|INSOLUBLE CARBONATE(38,4)\|MOLECULAR AMMONIA(37,15)\|ABSORBENT SLURRY(34,15)\|SLURRY(33,37)\|SILICATE(31,9)\|CARBON DIOXIDE CONVERSION(31,1)\|REACTOR CONTROL(31,1)\|WASHING CHAMBER(29,5)\|CARBON DIOXIDE RICH(28,4)\|RAW FLUE GAS(27,9)\|CARBONATE METAL SILICATE SLURRY(26,3)\|RESIDUAL AMMONIA SCRUBBER(23,5)\|INSOLUBLE METAL CARBONATE SILICA(23,2)\|REMOVING CARBON DIOXIDE(23,2)\|FLUE GAS(22,44)\|AMMONIUM CARBONATE SALT SOLUTION(22,7)\|POWER PLANT BOILER(21,5)\|SEQUESTRATION(21,5)\|MINERAL(19,10)\|CALCIUM HYDROXIDE(18,5)\|RETURN CHANNEL(18,4)\|CAVITY PRODUCTION(17,2)\|CHAMBER PRODUCT(17,2)\|FEEDER(17,2)\|AQUEOUS PHASE(16,22)\|SUBTERRANEAN CHAMBER(16,5)\|CARBONATION REACTION(15,4)\|MINERAL CARBONATION(15,3)\|CHILLED AMMONIATED SLURRY(15,1)\|SILICATE ROCK QUARRY(15,1)\|SOLUTION CIRCULATION(14,11)\|COAL FIRED POWER PLANT(14,6)\|UNDERGROUND CHAMBER(14,4)\|000MWE BITUMINOUS COAL(14,2)\|COOL AQUEOUS PHASE(14,2)\|METAL SILICATE SOLID(14,2)\|POWER PLANT(13,30)\|MIXED SOLUTION(13,3)\|HYDROSTATIC HEAD(13,2)\|AMMONIA RICH ORTHOCARBONATE(13,1)\|NONVOLATILE OXIDIZED MERCURY(13,1)\|CRUSHED LIMESTONE(12,2)\|HUNTER VALLEY(12,2)\|ABOVEGROUND PIPELINE(12,1)\|BOILER ECONOMIZER(12,1)\|FIN FAN COOLER(12,1)\|INSOLUBLE CARBONATED MINERAL(12,1)\|MINERAL SILICATESCARBON DIOXIDE(12,1)\|SERPENTINE QUARRY(12,1)\|STAGE CONCENTRATOR OVERFLOW(12,1)\|ULTRABASIC MINERAL(12,1)\|TEMPERATURE SILICATE SLURRY(10,3)\|AMMONIA ABSORPTION CHAMBER(10,2)\|CONCENTRATOR SEPARATION(10,2)\|ABOVEGROUND PIPING(10,1)\|CLARIFIER OVERFLOW(10,1)\|ENERGY THIRSTY TREND(10,1)\|GWH EMISSION(10,1)\|HYDRATED SALT GYPSUM(10,1)\|INCOMING SILICATE SLURRY(10,1)\|INSTALLATION CIRCUMSTANCE(10,1)\|MULTISTAGE CARTRIDGE PUMP(10,1)\|NITRATE ION ACCUMULATION(10,1)\|OLIVINE STONE(10,1)\|PREDOMINANT NATURALLY OCCURRING ADSORBATE(10,1)\|REACTOR SURROUNDINGS(10,1)\|TALL SCRUBBING CHAMBER(10,1)\|ULTRAFERRIERITE MINERAL(10,1)\|INSOLUBLE SOLID(9,4)\|AMMONIA LOSS(9,3)\|AMMONIA RECOVERY VESSEL(9,1)\|AMMONIA RICH AMMONIUM(9,1)\|BURNING BOILER(9,1)\|CONCENTRATOR REST(9,1)\|CONDENSING TOWER(9,1)\|DEINKING ASH(9,1)\|EQUILIBRIUM NITRATE(9,1)\|MAGNESIUM INGRESS(9,1)\|MAGNESIUM ION DISSOLUTION(9,1)\|MINE VOID(9,1)\|MINERAL CARBONATE(9,1)\|PERMANENTLY TREATING INSPECTED GAS(9,1)\|PYROXENE MINERAL(9,1)\|PYROXENE SILICATE MINERAL(9,1)\|SCRUBBING VESSEL(9,1)\|SERPENTINE STONE(9,1)\|SILICATE MINERAL QUARRY(9,1)\|SLURRY CIRCULATION(9,1)\|SPRAYER BANK(9,1)\|ULTRAMAFIC MINERAL(9,1)\|CONCENTRATION TANK(8,2)\|HYDROXIDE ION(8,2)\|PERMANENT PLACEMENT(8,2)\|PUMPING ENERGY(8,2)\|AQUEOUS SOLUTION(7,6)\|FLUE GAS FILTER(7,3)\|PRETREATMENT(7,2)\|SOLUBLE SALT(7,2)\|ALKALINE INDUSTRIAL RESIDUE(7,1)\|AMMONIA ABSORPTION CHILLER(7,1)\|AMMONIA MILLION(7,1)\|AMMONIUM CARBAMATE RICH SOLUTION(7,1)\|AMMONIUM SULFATE QUICKLIME(7,1)\|BURNING PAPER RECYCLING RESIDUE(7,1)\|CHILLING CAPACITY(7,1)\|CIRCULATING SOLUTION ACIDITY(7,1)\|COOLED FILTERED SMOKE(7,1)\|DISSOLVE TARGET(7,1)\|DIVALENT IRON ION(7,1)\|EXTRACTING(7,1)\|GAS XTHE(7,1)\|GEHO PUMP(7,1)\|INCOMING REACTION SLURRY(7,1)\|INORGANIC COMPONENT(7,1)\|INSOLUBLE MAGNESIUM HYDROXIDE PRECIPITATION(7,1)\|NITRATE RADICAL(7,1)\|PIPELINE REACTOR CHOICE(7,1)\|PREDOMINANT SALT(7,1)\|RELEVANT GOVERNMENT(7,1)\|RESIDUAL AMMONIUM SALT(7,1)\|RESIDUAL SOLUBLE SPECIES(7,1)\|SCRUBBING ZONE(7,1)\|SHOWER SPRAY(7,1)\|SIDESTREAM TREATMENT(7,1)\|SILICATE SLURRY FLOW CARBONATION(7,1)\|SPRAY HEADER(7,1)\|STACKED CAVITY(7,1)\|UNDERGROUND REACTOR PRODUCT(7,1)\|XSULFATE ION(7,1)\|FILTER CAKE(6,5)\|CARBON DIOXIDE SEQUESTRATION(6,4)\|CRITICAL LEVEL(6,3)\|ACTIVE SLURRY(6,2)\|CARBON DIOXIDE ABSORPTION CHAMBER(6,2)\|CARBON DIOXIDE EMISSION(6,2)\|ELECTRICITY(6,2)\|TEMPERATURE SLURRY(6,2)\|WOLLASTONITE(6,2)\|XBURNER(6,2)\|XCONVERSION(6,2)\|ABSORB EXCESS(6,1)\|AERATE LARGE SLURRY POND(6,1)\|ALKALI RICH SILICATE(6,1)\|AMMONIA COMPLEX(6,1)\|AMMONIA RICH SOLUTION(6,1)\|AMMONIATED SOLUTION(6,1)\|AMMONIUM BICARBONATE SALT(6,1)\|AMMONIUM SALT CIRCULATING SOLUTION(6,1)\|BICARBONATE ION(6,1)\|BICARBONATE REACTION(6,1)\|BOOSTER PUMP STATION(6,1)\|BYPRODUCT(6,1)\|CARBON DIOXIDE ADSORBATE(6,1)\|CARBONATE AMMONIUM BICARBONATE(6,1)\|CLASSIFICATION(6,1)\|CLEAR SUPERNATANT(6,1)\|CONCENTRIC TUBE(6,1)\|CONTAMINANT GAS(6,1)\|COUNTERCURRENT HEAT EXCHANGER(6,1)\|DENSITY SLURRY STREAM(6,1)\|DISSOLVED SPECIES(6,1)\|FEED GAS(6,1)\|FEED SLURRY(6,1)\|FEEDSTOCK(6,1)\|FILTER CLOTH(6,1)\|FINAL REACTION SLURRY(6,1)\|FLUE GAS DESULFURIZATION SCRUBBER(6,1)\|FRICTION LOSS(6,1)\|GAS INSPECTION(6,1)\|GYPSUM AMMONIUM HYDROXIDE(6,1)\|INSOLUBLE MATTER(6,1)\|MINERAL TRANSPORT(6,1)\|MIXING FLY ASH(6,1)\|NATURAL DRAFT COOLING TOWER(6,1)\|NEXT THICKENING TANK(6,1)\|ORTHOCARBONATE SALT METAL SILICATE SLURRY(6,1)\|OXIDIZING ENVIRONMENT(6,1)\|PREDOMINANT REACTION(6,1)\|PUMPING CAPACITY(6,1)\|RECOMBINATION REACTION(6,1)\|RECUPERATIVE HEAT EXCHANGER(6,1)\|RETURNING STREAM(6,1)\|SCRUBBED FLUE GAS(6,1)\|SESQUICARBONATE(6,1)\|STABLE MINERAL(6,1)\|STRATEGIC LOCATION(6,1)\|SULFUR CONTENT(6,1)\|WET GRINDING(6,1)\|SULFUR OXIDE(5,9)\|FILTRATION(5,3)\|MAGNESIUM CARBONATE(5,3)\|REACTION SOLUTION(5,3)\|UREA(5,3)\|COUNTER CURRENT DECANTATION(4,14)\|ACTIVATED AMMONIUM BICARBONATE METAL(4,1)\|AIR PREHEATING(4,1)\|AMMONIA CONTENT(4,1)\|AMMONIA RATIO(4,1)\|AMMONIA REMAINS(4,1)\|AMMONIA SOLUTION(4,1)\|AMMONIUM CARBONATE SALT RECOVERY(4,1)\|AMMONIUM ORTHOCARBONATE SALT SOLUTION(4,1)\|APPLICABLE EMISSION LIMIT(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWAVE POWER PLANT(4,1)\|BIOMASS(4,1)\|BLAST FURNACE(4,1)\|CARBON DIOXIDE ABSORPTION ZONE(4,1)\|CARBON DIOXIDE TENDENCY(4,1)\|CARBON DIOXIDE TON(4,1)\|CEMENT KILN(4,1)\|CHEMISTRY(4,1)\|CHILLED SOLUTION(4,1)\|COMMINUTION(4,1)\|CONVEYING METAL SILICATE SOLUTION(4,1)\|COOL GAS(4,1)\|COOLING WATER CIRCULATION(4,1)\|DOLOMITE(4,1)\|DOWNSTREAM GAS(4,1)\|ECONOMIZER SECTION(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|\|(IN6815/DELNP/2011)\|METHANEDIONE(100,70)\|SLURRY(100,37)\|PIPELINE(100,28)\|SILICATE SLURRY(100,14)\|METAL SILICATE SLURRY(100,13)\|METHANEDIONE SEQUESTRATION(100,12)\|FLOW PATH(100,9)\|GAS STREAM(100,9)\|SEQUESTRATION(100,8)\|CARBON SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|CARBON SEQUESTRATION(100,2)\|AMMONIUM 1 BICARBONATE METAL(100,1)\|BICARBONATE METAL(100,1)\|FLOW PATH PROVISION(100,1)\|REACTIVE AMMONIUM 1 BICARBONATE METAL(100,1)\|HARTSHORN(66,14)\|LIMESTONE PULVERIZATION(61,6)\|METHANEDIONE RICH FLUE GAS(60,2)\|REACTION SLURRY(54,17)\|METAL SILICATE(52,38)\|MAGNESIUM RICH SILICATE(44,8)\|PULVERIZED LIMESTONE INTRODUCTION(42,2)\|METHANEDIONE CAPTURE(42,1)\|BICARBONATE(41,13)\|METAL CARBONATE(41,11)\|HARTSHORN SOLUTION(38,4)\|REACTOR(37,27)\|CHESHUNT MIXTURE(35,48)\|METAL SILICATE ROCK(34,3)\|REACTION ENHANCEMENT(30,5)\|RECOVERED CHESHUNT MIXTURE(26,6)\|MOLECULAR AMMONIA(24,14)\|ABSORBENT SLURRY(23,15)\|SILICATE(21,10)\|RAW FLUE GAS(21,8)\|ECONOMIZER SECTION(19,3)\|CHESHUNT MIXTURE SOLUTION(18,10)\|SEPARATION SYSTEM(16,3)\|THICKENING TANK(15,8)\|RESIDUAL AMMONIA SCRUBBER(15,5)\|INSOLUBLE METAL CARBONATE SILICA(15,2)\|FLUE GAS STREAM(14,1)\|UNDERGROUND CHAMBER(13,8)\|OLIVINE(12,6)\|CARBONATE METAL SILICATE SLURRY(12,3)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|FLUE GAS(11,36)\|SOLUTION CIRCULATION(11,14)\|RECOVERY SYSTEM(11,3)\|CHAMBER PRODUCT(11,2)\|FEEDER(11,2)\|ULTRABASIC MINERAL(11,2)\|AQUEOUS PHASE(10,23)\|MINERAL CARBONATION(10,3)\|PRODUCING CHAMBER(10,2)\|CHILLED AMMONIATED SLURRY(10,1)\|CHILLING PLANT(9,3)\|BICARBONATE NH4HCO(9,2)\|COOL AQUEOUS PHASE(9,2)\|COOLING SYSTEM(9,2)\|HUNTER VALLEY(9,2)\|INCOMING SILICATE SLURRY(9,2)\|INEVITABLE BYPRODUCT(9,2)\|INSOLUBLE MAGNESIA(9,2)\|METAL SILICATE SOLID(9,2)\|METHANEDIONE SINK(9,2)\|MIXED SOLUTION(9,2)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|SERPENTINE QUARRY SITE(9,1)\|COAL FIRED POWER STATION(8,6)\|SULFATE ION(8,5)\|INSOLUBLE CARBONATE(8,3)\|THRESHOLD LEVEL(8,3)\|HOT SILICATE SLURRY(8,2)\|PERMANENT EMPLACEMENT(8,2)\|ULTRAMAFIC MINERAL(8,2)\|BLACK COAL MWE(8,1)\|CARBONATED MINERAL FINAL EMPLACEMENT(8,1)\|CENT METHANEDIONE(8,1)\|SPARINGLY SOLUBLE HYDRATED SALT(8,1)\|THICKENING STAGE(7,3)\|AMMONIA ABSORPTION CHILLER(7,2)\|FINAL PERMANENT REPOSITORY(7,2)\|FIRED ELECTRICITY GENERATION PLANT(7,2)\|METHANEDIONE CONTENT(7,2)\|CARBAMATE NH4COONH(7,1)\|CLARIFIED SUPERNATANT(7,1)\|CLARIFIER OVERFLOW(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|GASEOUS METHANEDIONE(7,1)\|INSTALLATION CIRCUMSTANCE(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|METHANEDIONE FAVOR FORMATION(7,1)\|MINERAL QUARRY SITE(7,1)\|MOLECULAR METHANEDIONE CO2(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|PRESSURIZED METHANEDIONE(7,1)\|QUICKLIME GYPSUM(7,1)\|SERPENTINE MG3SI2O(7,1)\|STACKED SUBCHAMBER(7,1)\|STAGE THICKENER OVERFLOW(7,1)\|TALL SCRUBBING CHAMBER(7,1)\|INSOLUBLE SOLID(6,4)\|AMMONIA LOSS(6,3)\|CARBON DIOXIDE(6,3)\|STATIC HEAD(6,2)\|AMMONIA RECOVERY VESSEL(6,1)\|AUSTRALIAN CONTEXT(6,1)\|CIRCULATING SOLUTION DELUGING SPRAY(6,1)\|DENSE SLURRY STREAM(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|INCOMING REACTIVE SLURRY(6,1)\|LIME CALCINATION(6,1)\|LJUNGSTROM ROTARY(6,1)\|MERCURY VAPOR(6,1)\|METHANEDIONE ABSORPTION CHAMBER(6,1)\|METHANEDIONE RICH GAS(6,1)\|MINERAL CARBONATE(6,1)\|PYROXENE MINERAL(6,1)\|PYROXENE SILICATE MINERAL(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|SCRUBBING VESSEL(6,1)\|SLURRY CIRCULATION(6,1)\|THICKENER BALANCE(6,1)\|POWER STATION SITE(5,8)\|SOX(5,7)\|FLUE GAS FILTER(5,3)\|REACTION CHAMBER(5,3)\|REACTION SOLUTION(5,3)\|AMMONIUM HYDROXIDE NH4OH(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|RETURN PIPELINE(5,2)\|SOLUBLE SALT(5,2)\|SOLUBLE SUBSTANCE(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA ABSORPTION CHAMBER(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CHILLING CAPACITY(5,1)\|CIRCULATING SOLUTION ACIDITY(5,1)\|CONCENTRIC PIPE(5,1)\|EMPLACEMENT CONTENT(5,1)\|FINAL THICKENER TANK(5,1)\|FUEL COMBUSTION(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|ION EQUILIBRIUM(5,1)\|IRON DISULFIDE FES(5,1)\|KEY CARBONATION REACTION(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|MOLL CO2(5,1)\|NATURAL SILICATE(5,1)\|NONVOLATILE MERCURIC OXIDE(5,1)\|OXIDIZING ENVIRONMENT(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRE METHANEDIONE(5,1)\|PRETREATMENT EXTENT(5,1)\|RAW SLURRY(5,1)\|RELEVANT GOVERNMENT(5,1)\|RESIDUAL STREAM CIRCULATION(5,1)\|SCRUBBING ZONE(5,1)\|SPRAY BANK(5,1)\|THICKENER SEPARATION(5,1)\|UNDERGROUND REACTOR PRODUCT(5,1)\|FILTER CAKE(4,5)\|ADJACENT FLOW PATH(4,2)\|FEED STREAM(4,2)\|FILTRATION MEDIUM(4,2)\|NILO2CO(4,2)\|PRECIPITATE(4,2)\|WOLLASTONITE(4,2)\|AMMONIATED SOLUTION(4,1)\|BICARBONATE ION(4,1)\|CARBONATION PRODUCT(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FILTER CLOTH(4,1)\|FINAL REACTION SLURRY(4,1)\|FLUE GAS DESULFURIZATION SCRUBBER(4,1)\|GAS TONNE(4,1)\|GEOLOGICAL CONDITION(4,1)\|IMPURITY GAS(4,1)\|MAGNESIUM ION(4,1)\|METHANEDIONE RATIO(4,1)\|METHANEDIONE SOURCE(4,1)\|MINERAL TRANSPORT(4,1)\|NEXT THICKENER TANK(4,1)\|PIPE REACTOR(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|POWER STATION BOILER ECONOMIZER(4,1)\|POWERFUL OXIDIZING AGENT(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECOMBINATION REACTION(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|REQUISITE EXTENT(4,1)\|SALT DISSOLUTION(4,1)\|SALT HYDRATION(4,1)\|SCRUBBING SOLUTION(4,1)\|SESQUICARBONATE(4,1)\|SLURRY FEED(4,1)\|SOLUTION OFNH4HCO(4,1)\|STRATEGIC LOCATION(4,1)\|STREAM RETURN(4,1)\|SUBSTANCE DISSOLUTION(4,1)\|SULFUR CONTENT(4,1)\|SULFUR DIOXIDE SO2(4,1)\|COUNTER CURRENT DECANTATION(3,15)\|2NH4HCO(3,1)\|6NH4HCO(3,1)\|AGITATION(3,1)\|AIR PREHEATING(3,1)\|ALIGNED CHAMBER(3,1)\|AMMONIA RATIO(3,1)\|AMMONIA RICH NORMAL CARBONATE(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|AQUEOUS PHASE CENT(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|CARBONATE RICH CHESHUNT MIXTURE(3,1)\|CASO4 2H2O(3,1)\|CHESHUNT MIXTURE SALT(3,1)\|CHILLED SOLUTION(3,1)\|CLEAR OVERFLOW SOLUTION(3,1)\|CONCENTRIC INNER(3,1)\|COOL GAS(3,1)\|COOLING WATER CIRCULATION(3,1)\|CRUSHING(3,1)\|DELUGE(3,1)\|DISCHARGE END(3,1)\|DOLOMITE(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|DRIVING MAGNESIUM(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|EXCESS AQUEOUS PHASE(3,1)\|FLY ASH SOLID(3,1)\|HEADER(3,1)\|HEAT CONSERVATION(3,1)\|HIGHLY EFFICIENT SCRUBBER(3,1)\|HYDROGEN ION CONCOMITANT FORMATION(3,1)\|INDICATIVE MASS BALANCE FIGURE(3,1)\|INORGANIC SOLID(3,1)\|INTERMEDIATE SALT(3,1)\|IRRADIATION(3,1)\|LIDDELL POWER STATION(3,1)\|LIMESTONE(3,1)\|LUMP PRODUCT(3,1)\|MAFIC ROCK(3,1)\|\|(AU2010210311)\|METHANEDIONE(100,65)\|SLURRY(100,37)\|METHANEDIONE SEQUESTRATION(100,10)\|GAS STREAM(100,6)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,3)\|HARTSHORN(90,13)\|LIMESTONE PULVERIZATION(83,6)\|METHANEDIONE RICH FLUE GAS(81,2)\|REACTION SLURRY(75,14)\|METAL SILICATE(69,33)\|MAGNESIUM RICH SILICATE(59,8)\|PULVERIZED LIMESTONE INTRODUCTION(57,2)\|METAL CARBONATE(56,9)\|HARTSHORN SOLUTION(56,3)\|METHANEDIONE CAPTURE(56,1)\|BICARBONATE(52,12)\|REACTOR(51,24)\|CHESHUNT MIXTURE(48,43)\|METAL SILICATE ROCK(46,3)\|REACTION ENHANCEMENT(41,5)\|RECOVERED CHESHUNT MIXTURE(36,6)\|MOLECULAR AMMONIA(33,14)\|ABSORBENT SLURRY(30,15)\|SILICATE(30,8)\|RAW FLUE GAS(28,8)\|CHESHUNT MIXTURE SOLUTION(26,9)\|ECONOMIZER SECTION(25,3)\|RESIDUAL AMMONIA SCRUBBER(21,5)\|SEPARATION SYSTEM(21,3)\|THICKENING TANK(20,8)\|INSOLUBLE METAL CARBONATE SILICA(20,2)\|BICARBONATE METAL(20,1)\|UNDERGROUND CHAMBER(18,8)\|CARBONATE METAL SILICATE SLURRY(18,2)\|FLUE GAS STREAM(18,1)\|OLIVINE(17,6)\|LAGGED ABOVEGROUND PIPELINE(17,1)\|METHANEDIONE PERMANENT SEQUESTRATION(16,1)\|RECOVERY SYSTEM(15,3)\|CHAMBER PRODUCT(15,2)\|FEEDER(15,2)\|ULTRABASIC MINERAL(15,2)\|AQUEOUS PHASE(14,22)\|SOLUTION CIRCULATION(14,13)\|MINERAL CARBONATION(14,3)\|PRODUCING CHAMBER(14,2)\|CHILLING PLANT(13,3)\|BICARBONATE NH4HCO(13,2)\|COOL AQUEOUS PHASE(13,2)\|COOLING SYSTEM(13,2)\|HUNTER VALLEY(13,2)\|INCOMING SILICATE SLURRY(13,2)\|INEVITABLE BYPRODUCT(13,2)\|INSOLUBLE MAGNESIA(13,2)\|METAL SILICATE SOLID(13,2)\|METHANEDIONE SINK(13,2)\|MIXED SOLUTION(13,2)\|CHILLED AMMONIATED SLURRY(13,1)\|SULFATE ION(12,5)\|CARBONATED SILICATE SLURRY(12,1)\|METHANEDIONE TONNE(12,1)\|SERPENTINE QUARRY SITE(12,1)\|INSOLUBLE CARBONATE(11,3)\|THRESHOLD LEVEL(11,3)\|HOT SILICATE SLURRY(11,2)\|PERMANENT EMPLACEMENT(11,2)\|ULTRAMAFIC MINERAL(11,2)\|THICKENING STAGE(10,3)\|METHANEDIONE CONTENT(10,2)\|CARBONATED MINERAL FINAL EMPLACEMENT(10,1)\|CENT METHANEDIONE(10,1)\|SPARINGLY SOLUBLE HYDRATED SALT(10,1)\|AMMONIA LOSS(9,3)\|AMMONIA ABSORPTION CHILLER(9,2)\|FINAL PERMANENT REPOSITORY(9,2)\|CARBAMATE NH4COONH(9,1)\|CLARIFIED SUPERNATANT(9,1)\|CLARIFIER OVERFLOW(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|FIN FAN COOLER(9,1)\|GASEOUS METHANEDIONE(9,1)\|ID MOLL CO2(9,1)\|INSTALLATION CIRCUMSTANCE(9,1)\|METHANEDIONE ABSORPTION ZONE(9,1)\|METHANEDIONE FAVOR FORMATION(9,1)\|METHANEDIONE ISOLATION(9,1)\|MINERAL QUARRY SITE(9,1)\|MOLECULAR METHANEDIONE CO2(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|QUICKLIME GYPSUM(9,1)\|STACKED SUBCHAMBER(9,1)\|STAGE THICKENER OVERFLOW(9,1)\|TALL SCRUBBING CHAMBER(9,1)\|INSOLUBLE SOLID(8,4)\|CARBON DIOXIDE(8,3)\|CARBON SEQUESTRATION(8,2)\|STATIC HEAD(8,2)\|AMMONIA RECOVERY VESSEL(8,1)\|AUSTRALIAN CONTEXT(8,1)\|CIRCULATING SOLUTION DELUGING SPRAY(8,1)\|DENSE SLURRY STREAM(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|H2O 2NH4HCO(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|INCOMING REACTIVE SLURRY(8,1)\|LIME CALCINATION(8,1)\|LJUNGSTROM ROTARY(8,1)\|MERCURY VAPOR(8,1)\|METHANEDIONE ABSORPTION CHAMBER(8,1)\|METHANEDIONE RICH GAS(8,1)\|MINERAL CARBONATE(8,1)\|PYROXENE MINERAL(8,1)\|PYROXENE SILICATE MINERAL(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|SCRUBBING VESSEL(8,1)\|SLURRY CIRCULATION(8,1)\|THICKENER BALANCE(8,1)\|POWER STATION SITE(7,8)\|SOX(7,7)\|COAL FIRED POWER STATION(7,5)\|FLUE GAS FILTER(7,3)\|MG3SI2O(7,3)\|REACTION CHAMBER(7,3)\|REACTION SOLUTION(7,3)\|AMMONIUM HYDROXIDE NH4OH(7,2)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|RETURN PIPELINE(7,2)\|SOLUBLE SALT(7,2)\|SOLUBLE SUBSTANCE(7,2)\|FILTER CAKE(6,5)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA ABSORPTION CHAMBER(6,1)\|AMMONIA MILLION(6,1)\|BOOSTER PUMPING STATION(6,1)\|CHILLING CAPACITY(6,1)\|CIRCULATING SOLUTION ACIDITY(6,1)\|CONCENTRIC PIPE(6,1)\|EMPLACEMENT CONTENT(6,1)\|FINAL THICKENER TANK(6,1)\|FIRED ELECTRICITY GENERATION PLANT(6,1)\|FUEL COMBUSTION(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INORGANIC COMPONENT(6,1)\|ION EQUILIBRIUM(6,1)\|IRON DISULFIDE FES(6,1)\|KEY CARBONATION REACTION(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|MON CO2(6,1)\|NATURAL SILICATE(6,1)\|NONVOLATILE MERCURIC OXIDE(6,1)\|OXIDIZING ENVIRONMENT(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRE METHANEDIONE(6,1)\|PRETREATMENT EXTENT(6,1)\|RAW SLURRY(6,1)\|RELEVANT GOVERNMENT(6,1)\|RESIDUAL STREAM CIRCULATION(6,1)\|SCRUBBING ZONE(6,1)\|SPRAY BANK(6,1)\|THICKENER SEPARATION(6,1)\|UNDERGROUND REACTOR PRODUCT(6,1)\|6NH4HCO(5,2)\|ADJACENT FLOW PATH(5,2)\|FEED STREAM(5,2)\|FILTRATION MEDIUM(5,2)\|LIMESTONE(5,2)\|PRECIPITATE(5,2)\|WOLLASTONITE(5,2)\|AMMONIATED SOLUTION(5,1)\|BICARBONATE ION(5,1)\|CARBONATION PRODUCT(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COUNTERCURRENT DECANTATION(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FILTER CLOTH(5,1)\|FINAL REACTION SLURRY(5,1)\|FLUE GAS DESULFURIZATION SCRUBBER(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|IMPURITY GAS(5,1)\|MAGNESIUM ION(5,1)\|METHANEDIONE RATIO(5,1)\|METHANEDIONE SOURCE(5,1)\|MINERAL TRANSPORT(5,1)\|NE4HCO SOLUTION(5,1)\|NEXT THICKENER TANK(5,1)\|PIPE REACTOR(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|POWER STATION BOILER ECONOMIZER(5,1)\|POWERFUL OXIDIZING AGENT(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECOMBINATION REACTION(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|REQUISITE EXTENT(5,1)\|SALT DISSOLUTION(5,1)\|SALT HYDRATION(5,1)\|SCRUBBING SOLUTION(5,1)\|SESQUICARBONATE(5,1)\|SLURRY FEED(5,1)\|STABLE MINERAL(5,1)\|STRATEGIC LOCATION(5,1)\|STREAM RETURN(5,1)\|SUBSTANCE DISSOLUTION(5,1)\|SULFUR CONTENT(5,1)\|SULFUR DIOXIDE SO2(5,1)\|SHELL(4,2)\|AGITATION(4,1)\|AIR PREHEATING(4,1)\|ALIGNED CHAMBER(4,1)\|AMMONIA RATIO(4,1)\|AMMONIA RICH NORMAL CARBONATE(4,1)\|ANNULUS(4,1)\|AQUEOUS PHASE CENT(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BIOMASS(4,1)\|CARBONATE RICH CHESHUNT MIXTURE(4,1)\|CLEAR OVERFLOW SOLUTION(4,1)\|CONCENTRIC INNER(4,1)\|COOL GAS(4,1)\|COOLING WATER CIRCULATION(4,1)\|CRUSHING(4,1)\|DELUGE(4,1)\|DISCHARGE END(4,1)\|DOLOMITE(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|DRIVING MAGNESIUM(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|EXCESS AQUEOUS PHASE(4,1)\|FLY ASH SOLID(4,1)\|FURNACE TEMPERATURE(4,1)\|HEADER(4,1)\|HEAT CONSERVATION(4,1)\|HIGHLY EFFICIENT SCRUBBER(4,1)\|HYDROGEN ION CONCOMITANT FORMATION(4,1)\|INDICATIVE MASS BALANCE FIGURE(4,1)\|INORGANIC SOLID(4,1)\|INTERMEDIATE SALT(4,1)\|IRRADIATION(4,1)\|LIDDELL POWER STATION(4,1)\|LUMP PRODUCT(4,1)\|	(WO2010/088738)\|Claims:\|1. A carbon dioxide sequestration process including the steps of:\|(i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium carbonate that is able to absorb the carbon dioxide, whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate;\|(ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|2. A process in accordance with claim 1, wherein the metal silicate rock is mixed the normal ammonium carbonate solution prior to absorbing the carbon dioxide in step\|3. A process in accordance with claim 1 or claim 2, wherein the reaction causes the bicarbonate in the presence of the metal silicate to partially decompose so as to produce an aqueous phase enriched in molecular ammonia and carbon dioxide.\|4. A process in accordance with claim 3, comprising the further step of cooling the aqueous phase such that free ammonia and carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered for re-use in step (i) of the process.\|5. A process in accordance with claim 4, comprising the further step of adding an alkali to the recovered ammonium carbonate in solution prior to being re-used in step (i).\|6. A process in accordance with claim 5, wherein the alkali is calcium oxide and/or hydroxide.\|7. A process in accordance with claim 6, wherein the calcium oxide is extracted from a flue gas stream prior to scrubbing in step (i).\|8. A process in accordance with any one of the preceding claims, comprising the further step of introducing pulverised limestone into a source producing the carbon- dioxide rich flue gasses.\|9. A process in accordance with claim 8, wherein the source is a coal-fired power station boiler and wherein the pulverised limestone is added upstream of an economiser section of the power station boiler.\|10. A process in accordance with claim 2, wherein a portion of the mixed solution used to scrub the gas stream prior to discharge to the atmosphere is chilled to ensure that a quantity of free ammonia in the gases is below a threshold level.\|11. A process in accordance with any one of the preceding claims, wherein the step of scrubbing the gas stream comprises exposing the carbon dioxide-containing gas stream to the solution as a spray.\|12. A process in accordance with any one of the preceding claims, wherein the step of controlling the reactor comprises elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\|13. A process in accordance with any one of the preceding claims, wherein the reactor is a pipeline.\|14. A process in accordance with claim 13, wherein the pipeline comprises multiple flow paths and wherein the reaction takes place along the length of one of the flow paths.\|15. A process in accordance with claim 14, wherein another of the flow paths is utilised to supply the metal silicate slurry to the first stage.\|16. A process in accordance with claim 15, comprising the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\|17. A process in accordance with any one of claims 1 to 12, wherein the reactor is a chamber located in use underground.\|18. A process in accordance with claim 17, wherein the chamber is located at a depth that provides sufficient pressure by way of static head to enhance the reaction between the carbon dioxide and the metal silicate.\|19. A process in accordance with any one of the preceding claims, comprising the further step of grinding a metal silicate rock to produce the metal silicate slurry.\|20. A process in accordance with claim 19, wherein the metal silicate slurry comprises approximately 25% by weight finely ground metal silicate solids.\|21. A process in accordance with any one of the preceding claims, wherein the metal silicate is a magnesium-rich silicate.\|22. A process in accordance with claim 21, wherein the magnesium rich silicate is a serpentine and/or olivine and/or pyroxene.\|23. A process in accordance with any of the preceding claims, comprising the further step of cooling the normal ammonium carbonate-metal silicate slurry prior to scrubbing.\|24. A system for sequestering carbon dioxide from a gas stream, the system comprising:\|(a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide\|reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and\|(b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|25. A system in accordance with claim 23, wherein the reactor is the pipeline as defined in any one of claims 13 to 16.\|26. A system in accordance with claim 23, wherein the reactor is the chamber as defined in any one of claims 17 or 18.\|27. A system in accordance with any one of claims 24 to 26, wherein the first apparatus comprises an absorption chamber arranged to circulate the normal ammonium carbonate solution through the carbon dioxide to thereby absorb the carbon dioxide.\|28. A system in accordance with any one of claims 24 to 27, wherein the reaction of the bicarbonate with the metal silicate further produces an aqueous phase containing molecular ammonia, carbon dioxide and water.\|29. A system in accordance with claim 28, further comprising a cooling arrangement arranged to cool the aqueous phase such that free ammonia and remaining carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered by a recovery arrangement of the system for re-use by the first apparatus.\|30. A system in accordance with claim 29, further comprising a control arrangement arranged to add a controlled amount of alkali to the recovered ammonium carbonate in solution prior to returning it to the first apparatus for re-use.\|31. A system in accordance with claim 29 or 30, further comprising a separation arrangement arranged to separate the recovered ammonium carbonate in solution from the insoluble metal carbonate-silica phase prior to recovery.\|32. A system in accordance with claim 31, wherein the separation arrangement comprises a counter-current decantation (CCD) system.\|33. A system in accordance with any one of claims 30 to 32, wherein the alkali is calcium oxide and/or hydroxide.\|34. A system in accordance with claim 33, wherein the calcium oxide is extracted from the raw flue gas stream prior to scrubbing.\|35. A system in accordance with any one of the preceding claims 24 to 34, comprising a feeder arranged to feed pulverised limestone at a source producing the carbon-dioxide rich flue gasses.\|36. A system in accordance with claim 35, wherein the point source is a coal-fired power station boiler and wherein the pulverised limestone is fed into raw flue gasses upstream of an economiser section of the power station boiler.\|37. A system in accordance with any one of claims 24 to 36, wherein the metal silicate comprises a magnesium rich silicate as defined in any one of claims 21 or 22.\|38. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica.\|39. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of:\|positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|40. A method in accordance with claim 39, wherein the slurry provided to the chamber is the reactive slurry produced in the process of any one of claims 1 to 12, or 19 to 22, when dependent on any one of claims 1 to 4.\|41. A method in accordance with claims 39 or 40, comprising the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber.\|42. A method in accordance with claim 41, wherein the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.\|43. A power station utilising a carbon sequestration system in accordance with any one of claims 24 to 37, the system arranged to sequester carbon dioxide from flue gas emitted by the power station.\|44. A method substantially as hereinbefore described with reference to the accompanying drawings.\|45. A system substantially as hereinbefore described with reference to the accompanying drawings.	(WO2010/088738)\|[0001] SYSTEM, APPARATUS AND METHOD FOR CARBON DIOXIDE\| [0002] SEQUESTRATION\| [0003] Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\| [0004] Background to the Invention\| [0005] There is increased focus on reducing carbon dioxide emissions to the atmosphere, to help minimise the effects of global warming. Carbon dioxide sinks exist naturally, with the main naturally occurring sink being the ocean. Plants are also an effective form of carbon dioxide sink and use photosynthesis to remove carbon from the atmosphere by incorporating it into biomass. However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\| [0006] A major source of harmful carbon dioxide gases are large fossil fuel power stations which, when fuelled by black coal, on average typically output around 0.8 to one tonne of the gas for each MegaWatt-hour (MWh) of electricity they generate. For example, a large power station such as the 2,640 MW Bayswater in the Hunter Valley of New South Wales, Australia, in generating 20 million MWh of electricity in a year, would also output 18 million tonnes of carbon dioxide. It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations. It would also be advantageous if a system and method were provided for the disposition of the gas to be independently audited in perpetuity.\| [0007] Summary of the Invention hi a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| [0008] (i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium carbonate that is able to absorb the carbon dioxide, whereby thecarbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate;\| [0009] (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| [0010] In the context of the present specification, the phrase "solution rich in normal ammonium carbonate " will be understood as referring to a solution whereby the main salt present corresponds to the formula for the normal form of ammonium carbonate\| [0011] (NILO2CO3.. There solution may, however, consist of other ammonium carbonate salts, and there may also be some molecular ammonia NH3, and ammonium hydroxide NH4OH, also present. Further, it should be noted that the terminology "gas stream containing carbon dioxide" does not mean that the stream contains only carbon dioxide, and may contain other off gases.\| [0012] hi an embodiment the metal silicate rock is mixed with the normal ammonium carbonate solution prior to absorbing the carbon dioxide in step (i).\| [0013] hi an embodiment the reaction causes the bicarbonate in the presence of the metal silicate to partially decompose so as to produce an aqueous phase enriched in molecular ammonia and carbon dioxide.\| [0014] hi an embodiment the method comprises the further step of cooling the aqueous phase such that free ammonia and carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered for re-use in step (i) of the process.\| [0015] hi an embodiment the method comprises the further step of adding an alkali to the recovered ammonium carbonate in solution prior to being re-used in step (i). The alkali may be calcium oxide and/or hydroxide, hi an embodiment the calcium oxide is extracted from gas stream prior to scrubbing in step (i).In an embodiment the method comprises the further step of introducing pulverised limestone into a source producing the carbon-dioxide rich gasses. The source may be a coal-fired power station boiler and the pulverised limestone is added upstream of an economiser section of the power station boiler.\| [0016] In an embodiment a portion of the mixed solution used to scrub the gas stream prior to discharge to the atmosphere is chilled to ensure that a quantity of free ammonia in the gases is below a threshold level. The threshold level may, for example, be set by the relevant government or other regulatory body.\| [0017] In an embodiment the step of scrubbing the gas stream comprises exposing the carbon dioxide-containing gas stream to the slurry as a spray or deluge operable to maximise the area of exposure between the slurry and the carbon dioxide-containing gas.\| [0018] In an embodiment the step of controlling the reactor comprises elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\| [0019] In an embodiment the reactor is a pipeline. The pipeline may comprise multiple flow paths and wherein the reaction takes place along the length of one of the flow paths. Another of the flow paths is utilised to supply the metal silicate slurry to the first stage.\| [0020] In an embodiment the method comprises the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\| [0021] In an embodiment the reactor is a chamber located in use underground. The chamber may be located at a depth that provides sufficient pressure by way of static head to enhance the reaction between the carbon dioxide and the metal silicate.In an embodiment the method comprises the further step of grinding a metal silicate rock to produce the metal silicate slurry. The metal silicate slurry may comprise roughly 25% by weight finely ground metal silicate solids.\| [0022] In an embodiment the metal silicate is a magnesium-rich silicate. In an embodiment the magnesium rich silicate is a serpentine and/or olivine and/or pyroxene mineral all commonly described as ultrabasic or ultramafic minerals.\| [0023] In an embodiment the method comprises the further step of cooling the normal ammonium carbonate-metal silicate slurry prior to it use in scrubbing carbon dioxide from flue gases.\| [0024] In accordance with a second aspect of the present invention there is provided a system for sequestering carbon dioxide from a gas stream, the system comprising: (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and\| [0025] (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\| [0026] In an embodiment the first apparatus comprises an absorption chamber arranged to circulate the normal ammonium carbonate solution through the carbon dioxide to thereby absorb the carbon dioxide.\| [0027] hi an embodiment the reactor is the pipeline as used in the method according to the first aspect.\| [0028] In an embodiment the reactor is the chamber used in the method according to the first aspect.In an embodiment the reaction of the bicarbonate with the metal silicate further produces an aqueous phase containing molecular ammonia, carbon dioxide and water.\| [0029] In an embodiment the system further comprises a cooling arrangement arranged to cool the aqueous phase such that free ammonia and remaining carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered by a recovery arrangement for reuse by the first apparatus.\| [0030] In an embodiment the system further comprises a separation system arranged to separate the recovered ammonium carbonate in solution from the insoluble metal carbonate-silica phase prior to recovery. The separation arrangement may, for example, be a counter-current decantation (CCD) system comprising one or more stages for separating the solution.\| [0031] In an embodiment the system further comprises a control arrangement arranged to add an alkali to the recovered ammonium carbonate in solution prior to returning it to the first apparatus for re-use.\| [0032] In an embodiment the alkali is calcium oxide and/or hydroxide. The calcium oxide is extracted along with other suspended solids (fly ash solids) from the gas stream prior to scrubbing.\| [0033] In an embodiment the system further comprises a feeder arranged to feed pulverised limestone into a source producing the carbon-dioxide rich flue gases. The point source may, for example, be a coal-fired power station and the pulverised limestone is fed into raw flue gases upstream of the power station boiler's economiser.\| [0034] In an embodiment the metal silicate comprises a magnesium rich silicate as used in the method according to the first aspect.In an embodiment the system further comprises an ammonium carbonate salt recovery arrangement arranged to recover ammonia and ammonium salts accompanying the final product.\| [0035] In an embodiment, the system comprises a solids-liquids separation system arranged to separate and recover ammonium carbonate salts, from the metal carbonate solid product that is sent for final emplacement.\| [0036] hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica.\| [0037] In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\| [0038] In an embodiment the slurry provided to the chamber is the reactive slurry produced in the process of the first aspect.\| [0039] In an embodiment the method comprises the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber.\| [0040] In an embodiment the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.In accordance with a fifth aspect there is provided a power station or other point source of carbon dioxide-rich flue gases, such as a blast furnace as used in steel making, or a cement kiln, utilising a carbon sequestration system in accordance with the second aspect, the system arranged to capture and sequester carbon dioxide from flue gas emitted by the power station or other point source.\| [0041] In accordance with a sixth aspect, in an ammonia absorption process in which a metal silicate rock is mixed with a normal ammonium carbonate salt solution in water so as to produce a normal ammonium carbonate salt solution in water/metal silicate slurry (the ammoniated slurry) for use in a carbon dioxide sequestration process, there is provided the step of chilling the ammoniated slurry to limit losses of ammonia in scrubbed flue gases to the extent necessary to meet emission limits applying at the location in question.\| [0042] hi an embodiment, the process comprises the further step of providing the ammoniated slurry to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammoniated slurry to thereby absorb the carbon dioxide into a reactive slurry.\| [0043] In accordance with a seventh aspect of the present invention there is provided a method of extracting a target metal from a metal silicate comprising the step of mixing the metal silicate with an ammonia-rich ammonium carbonate salt solution, and reacting the mixed solution to cause the target metal to dissolve into the solution.\| [0044] In an embodiment the method comprises the further step of grinding the metal silicate and forming it into a slurry prior to mixing the metal silicate with the solution.\| [0045] In an embodiment the metal silicate is a magnesium-rich silicate.\| [0046] hi an embodiment the magnesium-rich silicate is a serpentine and/or olivine and/or pyroxene silicate mineral commonly described as an ultrabasic or ultramafic mineral.In an embodiment the solution comprises normal ammonium carbonate salts dissolved in water (the ammoniated solution).\| [0047] In an embodiment the target metal dissolves into the solution and then precipitates in the presence of carbon dioxide, as a metal carbonate to be removed for recovery.\| [0048] In an embodiment the target metal is one or more of magnesium, calcium or iron. The dominant metal within the metal silicate may comprise magnesium.\| [0049] In an eighth aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| [0050] (i) in a first stage, mixing a slurry of a metal silicate rock with a normal ammonium carbonate solution so as to produce a normal ammonium carbonate salt/water/metal silicate slurry;\| [0051] (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the chilled solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| [0052] (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\| [0053] Brief Description of the Drawings\| [0054] An embodiment of the present invention will now be described, by way of example only, with reference to the accompanying drawings, in which:\| [0055] Fig. 1 is a schematic of a carbon dioxide sequestration system according to an embodiment of the present invention;\| [0056] Fig. 2 is a schematic of a carbon dioxide sequestration system according to an alternative embodiment of the present invention;\| [0057] Fig. 3 is a process flow diagram showing a method of sequestering carbondioxide using the system of either Fig. IA or IB, in accordance with an embodiment of the present invention;\| [0058] Fig. 4 is a schematic of a heat exchange apparatus, in accordance with an embodiment of the present invention;\| [0059] Fig. 5 is a schematic of a pressure exchange apparatus in accordance with an embodiment of the present invention; and\| [0060] Fig. 6 is a schematic illustrating a metal silicate preparation and grinding technique, in accordance with an embodiment of the present invention.\| [0061] Detailed Description of an Embodiment\| [0062] In the following description, embodiments of the present invention are described in the context of a system, apparatus and method for the capture and sequestration of carbon dioxide contained within flue gases emitted by a fossil fuel-fired power station. However, it is to be understood that the system, apparatus and method could equally be utilised for the permanent sequestration of carbon dioxide from any 'point' source and is not limited to the particular arrangement described herein. With reference to Fig. 1 there is shown a flow diagram of a system 10 for performing a carbon dioxide (CO2) sequestration process from a gas feed stream containing carbon dioxide outputted from a power station, in accordance with a first embodiment of the present invention. With additional reference to Fig. 3, the system 10 is arranged to perform the process 100 of (i) scrubbing a gas stream containing carbon dioxide with a normal ammonium carbonate solution that is able to absorb the carbon dioxide, whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising, in the main, ammonium bicarbonate; and (ii) passing a slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| [0063] In an embodiment the method may further comprise a stage (iii) of contacting flue gases with a circulating dilute normal ammonium carbonate solution that may be chilled to the extent necessary, in a vessel in a counter-current, staged manner so thatresidual ammonia in the flue gases is scrubbed from these gases to levels low enough to allow their final discharge in the atmosphere.\| [0064] In the illustrated embodiment the stages (i) and (iii) are performed within a first apparatus 20 having separate chambers, in the form of an absorption chamber 28 and a scrubbing chamber 30, respectively. Stage (ii) occurs within a reactor either in the form of a pipeline 52 (as shown in Fig. 1) or, as will be described in more detail in subsequent paragraphs with reference to Fig. 2, an underground chamber excavated at a sufficient depth to facilitate conditions for the carbonation reactions to take place. According to Fig. 1, the pipeline 52 may connect the reactor to a mineral quarry site from with metal silicate is sourced.\| [0065] The carbon dioxide sequestration process utilised in embodiments of the present invention is based on mineral carbonation. Mineral carbonation is a reaction between a metal-oxide-bearing mineral material and carbon dioxide. The metal-oxide bearing material may, for example, be alkaline-earth metals. Advantageously, the process 100 does not require the source of carbon dioxide to be particularly pure. In mineral carbonation, carbon dioxide reacts with the metal oxide bearing material to generate insoluble carbonates, that is to say:\| [0066] MO + CO2 → MCO3 + heat (1)\| [0067] which is an exothermic reaction, occurring more rapidly at elevated temperature, typically above 1500C. Certain chemicals may serve to increase the rate at which this reaction proceeds without being consumed themselves, i.e. they serve as catalysts. The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage). Further, embodiments are inherently operable to make bicarbonate ions as carbon dioxide is absorbed into the ammonia-rich ammonium carbonate solution, without having to handle highly pressurized carbon dioxide.\| [0068] The exact nature of the insoluble carbonates formed by the reaction depends on the metal-oxide bearing material. Suitable materials may be naturally occurring alkaline-earth metal-rich silicate rocks which contain mineral constituents such asserpentine (Mg3Si2O5(OH)4), olivine (Mg2SiO4), orthopyroxene (MgSiO3), talc (Mg3Si4O10(OH)2) and wollastonite (CaSiO3). In practice, the element Iron (Fe) may substitute for some of the Magnesium (Mg) or Calcium (Ca). Other suitable materials include alkaline industry residues such as slag from steel production, the ash (both fly and bottom) from pulverised coal-fired boilers, the ash remaining from the combustion of paper recycling residues (de-inking ash), and cement. The amount of heat generated in the reaction will depend on the specific metal and on the mineral containing the metal oxide as can be seen below in the case of three natural silicates (heat values are given per unit mole of CO2 and at standard conditions (25°C and 0.1 MPa):\| [0069] Olivine\| [0070] Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 + 89 kJ moll CO2 (2a)\| [0071] Serpentine Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol" 1 CO2 (2b)\| [0072] Wollastonite\| [0073] CaSiO3 + CO2 → CaCO3 + SiO2 + 90 kJ mol l CO2 (2c)\| [0074] In the illustrated embodiments, the silicate rock comprises the mineral serpentine, Mg3Si2O5(OH)4. AU of the above minerals may be pre-treated to increase the surface area of rock that can subsequently come into direct contact with the carbon dioxide. In an embodiment, the pre-treatment involves crushing, grinding and/or milling of the mineral, as well as some mechanical classification and separation. For example, the minerals could be milled (e.g. wet-milled) in ball mills or equivalent to form a finely ground metal silicate slurry (hereafter 'silicate slurry') 36 wherein 90% of the mineral matter is finer than 40 microns. However, it will be understood that the extent of the pre-treatment is dependent upon the source and type of mineral(s) being used in the process. An example milling and transportation process flow is shown in Fig. 6.\| [0075] Again with specific reference to Fig. 1, the carbon dioxide sequestration system 10 will now be described in detail. The system 10 receives a raw flue gas mixture feed stream 32 that has been generated and subsequently emitted by a powerstation or other point source (not shown). In the embodiment described herein, the raw flue gas mixture 32 is passed though a filter 33 to remove most of the particulate matter. Suitable filters may include fabric filters, electrostatic precipitators and the like. Cleaning the raw flue gas mixture 32 may serve to minimise both the maintenance costs in downstream gas-handling equipment and the concentrations of particulates in flue gases ultimately discharged to the atmosphere. It will be understood, however, that while desirable for process reasons, it is not essential that the raw flue gas mixture 32 be cleaned of all particulates before it enters the scrubbing chamber 30. In an embodiment, the filtering process may additionally involve controlling the level of SOx and NOx that is present within the flue gas so as to adjust the pH level of the ammoniated slurry by virtue of the concentration of sulfate and nitrate ions present in it (which in turn affects the reaction rate between the silicate rocks and carbon dioxide by driving magnesium and calcium ions into solution) as will be described in detail below.\| [0076] To maximise heat recovery in the system 10, the filtered flue gas mixture is then passed through a heat exchange apparatus in the form of a heat exchanger 34 so that the sensible heat of the filtered flue gas mixture (typically at a temperature of around 135°C) is exchanged with the cooler gasses being expelled from the scrubbing chamber 30 of the first apparatus 20 and the filtered flue gas mixture is cooled to its water-vapour saturation temperature (i.e. to about 50°C). Suitable heat exchangers may include, for example, recuperative-type heat exchangers, such as the Ljungstrom rotary design as commonly used for air pre-heating in power stations.\| [0077] As mentioned in preceding paragraphs, the carbon dioxide sequestration system 10 receives a source of silicate slurry 36. According to the embodiment described herein, the silicate slurry source is located near or at the mine site from which the silicate rocks are sourced. As previously described, the silicate mineral sourced from the mine site is finely ground (e.g. by wet-milling in ball mills or equivalent to form the slurry) wherein roughly 90% of the mineral matter is finer than 40 microns or as determined to be appropriate for the proper operation of the process.\| [0078] According to Fig. 1, the silicate slurry 36 is first blended with a solution in water of normal ammonium carbonate to create an ammonia rich ammonium carbonate- metal silicate slurry (hereafter "absorbent slurry"). In the illustrated embodiment, the normal ammonium carbonate salts in solution (hereafter "circulating solution") is the solution in water of most of the normal ammonium carbonate salts accompanying thefinal metal carbonate/silica product. Specifically, according to the Fig. 1 embodiment, the circulating solution represents the overflow of a first thickener 90a of a counter- current decantation (CCD) thickener separation system 90.\| [0079] In flowing from the CCD thickener system 90 to the power station site, the absorbent slurry 47 passes through a first pressure-exchange apparatus 38. To minimise power consumption, the pressure of the absorbent slurry 47 may be increased by exchanging pressure with the final metal carbonate/silica product (hereafter 'final product'), typically to a pressure of approximately 100 Bar. hi addition, to minimise heat losses from the system 10 (and to ensure that the final product is cooled to a suitable temperature before it is emplaced in its final permanent repository), the absorbent slurry 47 passes counter-currently through a heat exchanger 40 to absorb the surplus sensible heat contained in the final product.\| [0080] According to Fig. 1, a pipeline 44 connects the first apparatus 20 to the silicate mineral quarry site and is used to transport the absorbent slurry 47 used in the sequestration process 100. As will be described in more detail in subsequent paragraphs, an alternate path 52 in the pipeline 44, in this embodiment, also serves to act as a controlled reactor in which the metal carbonation reaction largely takes place. At or near to the power station site, the absorbent slurry 47 is passed counter-currently through a second heat exchanger 46 and a second pressure-exchange apparatus 48, where the absorbent slurry 47 is cooled and reduced in pressure by exchange with the reactive slurry discharged from the first apparatus 20, before being fed directly into the scrubbing chamber 30.\| [0081] After arriving at the power station site, a residual circulating stream passes into a vessel in the form of a residual ammonia scrubber 56, in such a way that flue gases that have been stripped of most of their carbon dioxide content, pass upwards from below. There may be any number of counter-current contacting stages, depending only on the desired implementation. The residual ammonia scrubber 56 is operable such that the cleaned, largely carbon dioxide-free flue gases may leave the system with less than one part per million of ammonia, hi order to achieve such low losses of ammonia, the fluid circulating through this vessel may be cooled, even chilled, to an appropriate degree. Specifically, the fluid circulating through this vessel is comprised of the dilute aqueous phase described above (i.e. a clarified, dilute solution in water of normal ammonium carbonate), which enters the vessel and collects in the base of the residualammonia scrubber 56 from where it is circulated by pumps to the header sprays to above the uppermost of the contacting stages. It is this circulating flow that is cooled to the requisite extent, by firstly, arranging for it to flow firstly, through one or more first stage heat exchangers that are cooled by circulating water cooled in turn, in a cooling tower, and secondly, through one or more second-stage heat exchangers that are cooled in turn, by a stream of water or other suitable heat-exchange fluid that has been chilled to below ambient temperatures by a chilling plant suitable for the purpose. In an embodiment, the chilling plant is an ammonia absorption chiller 82, the operating principles of which are understood by those skilled in the appropriate art. It is to be understood however, that alternative types of chilling plant provided they have adequate chilling capacity, are equally suitable.\| [0082] Absorption chillers, including ammonia absorption chillers, require a source of heat for their operation. In an embodiment, some of this heat may be provided by the heat released through carbonation reactions as shown as equations 2a, 2b and 2c, depending on the type of silicate mineral used.\| [0083] The cooled filtered flue gas mixture passing through the heat exchanger 34 enters the scrubbing chamber 30 where the gas mixture passes upwards through deluging sprays of circulating solution entering from the residual ammonia scrubber 56 from above. When carbon dioxide is absorbed in the circulating solution, a further substantial quantity of heat is liberated, as gaseous carbon dioxide is absorbed into it, and reacts with the normal ammonium carbonate salts in the circulating solution. The reactions include the conversion of the normal ammonium carbonate (NELt)2CO3 to the bicarbonate NH4HCO3, via the reaction:\| [0084] (NFLt)2CO3 + CO2 + H2O -» 2NH4HCO3 (3)\| [0085] Normal ammonium Ammonium\| [0086] Carbonate bicarbonate\| [0087] While this will be the main reaction encountered, other reactions may equally occur in parallel including, when there is free molecular ammonia present in the scrubbing solution:\| [0088] NH3 + CO2 + H2O -> NH4HCO3 (3a)As well, some of the ammonium bicarbonate may lose some combined water to form the carbamate, NH2COONH4, hence this compound will likely be present in smaller quantities, perhaps along with some urea, CO(NH2)2, formed when the carbamate loses additional combined water.\| [0089] FURTHER DETAIL OF SEQUESTRATION PROCESS\| [0090] In more detail, the carbon capture process begins with the metal silicate (in this case, ground serpentine) being blended into a circulating solution of serpentine and an aqueous phase containing normal ammonium carbonate in solution to thereby produce the absorbent slurry. The absorbent slurry is then circulated using pumps, through a carbon dioxide absorption chamber 28 which in an embodiment may be the lower half of a tall scrubbing chamber 30 (the upper part being utilised as the residual ammonia scrubber 56). The absorption chamber 28 may, for example, take the form of a flue gas desulfurization scrubber, with the absorbent slurry circulated at high flow rates through banks of sprays.\| [0091] The absorbent slurry is heated by the transfer of latent heat from the flue gases rising from below. Also, as mentioned above, when carbon dioxide gas is absorbed into the absorbent slurry, substantial quantities of heat are liberated, as carbon dioxide reacts with the mainly normal ammonium carbonate (NHi)2CO3, to form the bicarbonate NH4HCO3, as per Equation 3 (there may also be some intermediate salts e.g. the sesquicarbonate (NFLO2CO3. NH4HCO3, the carbamate NH4COONH2, and traces of urea, CO(NH2)2). The heat of solution, along with the latent heat released when water vapour in the flue gases condenses, is removed by circulating the absorbent slurry through water-cooled heat exchangers 84.\| [0092] As mentioned above, the output from the absorption chamber 28 is a reactive solution in the form of a metal silicate slurry in an aqueous phase that is itself a solution of carbonate-rich ammonium carbonates, primarily ammonium bicarbonate. A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor.On route to the mine site, at or near to the power station, the reactive slurry is pressurised at the second pressure-exchange apparatus 48 to a high pressure of around 120 Bar (above the critical pressures of both carbon dioxide and ammonia) and also heated to at least 100°C and preferably to at least 150°C. Heating is accomplished by transferring heat from the incoming silicate slurry arriving from the mine at the heat exchanger 46, and also, if necessary, by injection of steam 54. The heat contained in the incoming silicate slurry in part originates from reactions 2(a), 2(b), and 2(c), depending on the silicate mineral involved. hi the return pipeline 52 of the pipe reactor, at temperatures below 50°C or thereabouts, most if not all of the carbon dioxide present is in the form of ammonium carbonates. When the slurry is heated to at least 100°C under pressures of at least 100 Bar, the tendency is for the various forms of ammonium carbonates in solution to decompose to molecular carbon dioxide CO2 and ammonia NH3. These remain substantially in solution in the reactive slurry under these temperature and pressure conditions. A result of this process is the partial pressure of the carbon dioxide will be particularly high, thereby serving to enhance the speed of reaction with the silicate minerals, converting them to insoluble carbonates and silica during the transit. In an embodiment, the pipeline may be 10 kilometres in length to allow adequate time for the reactions to proceed essentially to completion resulting in the metal carbonate product that contained most if not all of the carbon dioxide originally scrubbed from the power station flue gases. It will be understood that the length may vary, however, depending on the actual implementation.\| [0093] It will be apparent that a high concentration of ammonia is maintained in the slurry throughout its passage from the power station to the silicate rock mine/quarry or other emplacement site.\| [0094] When the final product in the return pipeline 52 reaches the vicinity of the mine site, as described above, the hot pressurised final product transfers its sensible heat via the heat exchanger 40 to the absorbent slurry being pumped towards the power station, hi the process the final product is cooled to a temperature below 50°C. To achieve this temperature in practice, it may be necessary to employ additional cooling to ensure that the temperature of the final product stream is cool enough for the recombination reactions to occur. In an embodiment, the additional cooling is accomplished by means of a heat exchanger cooled by circulating cooling water fromdry (e.g. radiator-type) cooling towers, fin fan coolers, or a natural-draft cooling tower (not shown) such as used for cooling in the power station. A consequence is that free molecular ammonia and carbon dioxide will subsequently re-combine to form ammonium carbonate salts dissolved in the aqueous phase that can be recovered and used in the circulating solution. Since carbon dioxide has been removed from the aqueous phase by reaction with the mineral silicate, the ratio of carbon dioxide to ammonia is lower than it was before the key carbonation reactions occurred. Hence, the predominant form of ammonium carbonate salt formed is normal ammonium carbonate (NKU)2CO3 which, it will be noted, may contain twice as many ammonia units pre carbon dioxide unit as the bicarbonate, NH4HCO3. This is the reason why a solution rich in normal ammonium carbonate may also be referred to as an ammonia-rich ammonium carbonate solution. In any case, it will be understood that other ammonium salts, plus molecular ammonia NH3 and ammonium hydroxide NH4OH, may also be present.\| [0095] FURTHER DETAIL OF SEPARATION SYSTEM\| [0096] As previously mentioned, the final reacted slurry (i.e. containing mainly normal ammonium carbonate in solution together with the carbonate/silica solids that are the products of carbonation) is passed through a solids-liquids separation process. The separation process generally involves producing a clear overflow solution containing most of the ammonium salts and other soluble chemicals (including any molecular ammonia and ammonium hydroxide NH4OH that are dissolved in it) and a dense slurry or even paste-consistency underflow containing all of the solids.\| [0097] Separation may be accomplished by one or more of several means known to those skilled in the art. In an embodiment, a filtration process may be employed using, for example, rotary vacuum filters. In an alternative embodiment, the filtration process may use plate and frame-type filter presses. In both embodiments, a filter cake is formed on a filtration medium (a filter cloth for example) and wash-water is sprayed onto, or otherwise caused to pass through, the filter cake to wash out residual quantities of soluble materials including ammonium carbonate salts. The filter cake represents the first, solids-rich stream, which may be handled as a cake, or converted to a dense slurry by addition of small quantities of additional water sufficient to allow it to be handled asa slurry. The aqueous phase, including wash-water passing through the filter cake and filtration medium, represents the second stream. In another embodiment, separation of the solids from the aqueous phase (specifically, the separation of the ammonium carbonate salts and other soluble materials in the aqueous phase) is achieved by a process known as counter-current decantation (CCD), as illustrated in the Fig. 1 and 2 embodiments. This technique involves utilising a number of continuous thickener tanks (in the illustrated embodiment three tanks are used, although it will be understood by persons skilled in the art that more or less thickener tanks may be employed depending on the desired implementation) that are arranged in a series. The CCD thickener system 90 may recover a substantial amount (e.g. around 99 per cent) of all of the dissolved salts and other soluble substances (including ammonia) in the aqueous phase accompanying the final product. The remaining amount of salts will accompany the final product solids as they are pumped to their final permanent repository.\| [0098] It is noted that in some implementations, only a certain percentage (e.g. 80%) of soluble substances may be recovered by the first thickener 90a of the CCD system 90, with the remainder recovered by subsequent stages. In an embodiment, as shown in Figure 1, the two aqueous-phase streams resulting from the overflows of the first-stage and second-stage thickeners are blended either by arranging for the overflow of the second stage thickener to be blended with the feed stream to the first-stage thickener, or by directly blending the two overflow streams.\| [0099] In more detail, the final products stream from the reactor, after pressure reduction in the pressure exchangers 38 and cooling in the heat exchangers 40, enters the first thickener 90a of the series. The insoluble solids (the carbonated mineral) suspended in the feed stream settle in the thickener tank 90a to form a dense slurry that is withdrawn as an underflow stream. The balance of the feed entering the thickener tank overflows as a clarified supernatant, which contains most of the soluble ammonium carbonate salts and other soluble materials (i.e. the circulating solution). The underflow may still contain around 10 per cent of the aqueous phase that first entered the thickener, and it is the function of the balance of thickeners in the CCD system to recover these salts to the maximum practicable extent, from the insoluble solids that are to be finally emplaced. In the CCD system 90, the underflow slurry from thickener tank 90a is pumped to the next thickener tank 90b in line. Also fed to tank 90b is the clarified overflow from thickener tank 90c, and so on. Where "N" thickenertanks are employed, the final thickener tank in the series, tank N, receives a feed stream which is a mixture of the underflow of thickener tank N-I, and fresh water, which may be replaced in part by any surplus aqueous phase recovered from final emplacements of carbonated mineral as this further consolidates and/or drains from the mineral, over time. In an embodiment, a mixture of thickener tanks, one or more stages in series, and filtration units may be used to effect the separation of soluble ammonium carbonate salts from the insoluble carbonated mineral.\| [0100] The dense slurry stream (in one embodiment a filter cake, in another embodiment the underflow of CCD thickener Unit N) is the final product slurry substantially free of salts, and in a form suitable for permanent emplacement in mine voids or other purpose-built repositories (not shown). In these emplacements the solids can settle and consolidate, releasing additional aqueous phase as a clear supernatant. This supernatant may also be collected and re-used in the process, as described in the paragraph above. When the CCD system 90 for the recovery of ammonium salts is close to the power station, as may be the case for the underground chamber reactor embodiment (Fig. 2), it may be appropriate to add the remainder of the power station fly ash to the final product slurry from the carbon sequestration process, so the two streams may be handled and co-disposed of as a single stream. An advantage stemming from the presence of fly ash having pozzolanic properties (a tendency to "set" in the presence of alkalis and moisture) in the final product, is that it will assist with the rehabilitation process, by encouraging the final product/fly ash mix to "set", thereby immobilising the contents of the emplacement. hi an embodiment the overflow of the second stage of the CCD thickener system 90, being a relatively dilute, clarified (insoluble solids- free) solution in water of ammonia-rich ammonium carbonate salts may be handled separately (see Fig. 2). hi such an embodiment, the stream (hereafter "residual stream") is sent overland from the CCD system 90 (installed near the silicate quarry) to the power station site via a separate, third pipeline 91. Pumps raise the pressure of the contents of the third pipeline 91 to the extent necessary for them to traverse the length of the pipeline 91. However, it will be understood that the third pipeline 91 may be configured to accept some of the heat and some of the pressure energy released when the pressure and temperature of the final products pipeline are reduced via heat- and pressure-exchange equipment.Whether the third pipeline 91 is configured in this way, or simply used as a conduit for the return of this stream to the power station site, depends on the individual circumstances of the installation.\| [0101] 5 CHEMICAL REACTIONS\| [0102] The main chemical processes occurring throughout the process are as follows: 3CO2 + 3(NH4)2CO3 + 3H2O -» 6NH4HCO3 (4)\| [0103] 6NH4HCO3 -> 6NH3 + 6H2O + 6CO2 (5)\| [0104] 6CO2 + Mg3Si2O5(OH)4 -» 2SiO2Φ + 3MgCO3Ψ + 2H2O 0 + 6NH3 + 3CO2 (6)\| [0105] 3CO2 + 6NH3 + 3H2O -» 3(NILO2CO3 (7)\| [0106] NH3 + NH4HCO3 -» (NILO2CO3 (8)\| [0107] Equation 4 represents the absorption of carbon dioxide into the ammonia-rich5 ammonium carbonate aqueous phase to produce a solution comprising ammonium bicarbonate. On heating under pressures of at least 100 Bar in the reactor (i.e. pipeline or underground chamber), this ammonium bicarbonate decomposes to molecular ammonia, water and carbon dioxide according to equation 5. As shown in equation 6, under the high pressure and temperature conditions prevailing in the reactor the carbon O dioxide reacts with the serpentine (the chemical formula of which is shown in equation 6) or other silicate rock to form insoluble metal carbonates and silica, the final products of the process, which store the carbon dioxide. Equation 7 describes what happens after the reaction products are cooled to below 50°C, i.e. low enough to allow the free molecular ammonia and carbon dioxide to combine to form ammonium carbonate salts5 in solution. As shown, since much of the carbon dioxide has been absorbed by the metal silicate (here serpentine) the ratio of ammonia to carbon dioxide favour formation of the ammonia-rich normal carbonate. Additional normal ammonium carbonate may form according to equation 8, by reaction between ammonium bicarbonate, and free molecular ammonia. 0CONTROLLING ACIDITY IN THE SYSTEM\| [0108] As mentioned in preceding paragraphs, sulfate ions from SOx, and nitrate ions from NOx respectively, contained in the raw flue gases, may accumulate in the circulating solution of ammonium salts. Oxides of sulfur (SOx) are inevitable byproducts of the combustion of fossil fuels including coal, that incorporate sulfur- containing compounds in reduced form, for example pyrite (iron disulfide FeS2). Oxides of nitrogen (NOx) are also inevitable byproducts of the combustion of fossil fuels including coal, originating from nitrogen-containing compounds in the fuel, and from reactions between oxygen and nitrogen in air induced by the heat of the fuels' combustion, hi an Australian context, where coals tend to have low sulfur contents, and assuming use of modern "low-NOx burners", the rates of build-up of nitrate ions will not be high, but their build-up may still need to be limited to maintain the pH range to that most suited for the overall processes. When the SOx and NOx contained in flue gases contact the absorbent slurry as encountered in the scrubbing chamber 30 in the presence of additional oxygen including that contained in flue gases, a series of reactions occur that convert these gases to sulfates and nitrates: SOx to sulfate ions SO4— , and NOx to nitrate ions NO3-. In the normal course of separating out the insoluble solids for example magnesite and silica formed from the reactions between carbon dioxide and the metal silicates, as previously described, the soluble salts dissolved in the aqueous phase from the reactor including sulfates and nitrates are recycled for re-use in the scrubber, apart from the small quantities of such salts that are ultimately emplaced with the final product metal carbonates and silica. A consequence is that while carbon dioxide entering the system forms additional carbonate ions that are ultimately removed at an equal rate as insoluble metal carbonates, the tendency is for both sulfate and nitrate ions to accumulate in the circulating aqueous phase. In an embodiment, the system may implement a process for limiting the build-up of these ions (anions) to avoid an increase in the acidity (reduction in the pH number) of the circulating solution, as the formation of these ions leads to a concomitant formation of hydrogen ions in solution. It is noted that the system, to some extent, may inherently limit such a build-up by virtue of the fact that, as mentioned in the previous paragraph, not all soluble salts and other dissolved substances will be recovered by way of the solids-liquids separationprocess. To further reduce nitrate ion equilibrium concentration, it is necessary to limit correspondingly, the concentrations of NOx gases in the flue gases entering the scrubbing vessel 30. This may be achieved, for example, by using so-called 'low-NOx burners', and by other methods which achieve control of the combustion process to limit NOx formation in the power station's boilers.\| [0109] To control concentrations of sulfate ions in the circulating aqueous phase, the system 10 may employ an additional control mechanism 96 arranged to add/feed appropriate quantities of calcium oxide or hydroxide (which in water form calcium ions and hydroxyl ions) to a portion of the circulating slurry (a side-stream), wherein the sulfate ions react with it to form calcium sulfate, which mostly precipitates out as the sparingly soluble hydrated salt, gypsum:\| [0110] SO4" + Ca+* + 2H2O -» CaSO4.2H2O Ψ (9)\| [0111] Meanwhile, the hydroxyl ions combine with and neutralise a corresponding number of hydrogen ions (to form water molecules), thereby controlling (reducing) the acidity of the circulating solution.\| [0112] In an embodiment, calcium oxide generally may be naturally present in the power station fly ashes. If present in sufficient concentrations, the appropriate quantities of fly ash may be added by the control mechanism 96 to the circulating solution to control the pH levels to the desired ranges. If the quantities of calcium oxide naturally present in fly ash are inadequate, they may, in an embodiment, be augmented by adding pulverised limestone to raw power station flue gases in the boilers at one or more locations for example immediately upstream of the economiser section of the boilers, where flue gas temperatures are appropriate for the decomposition of limestone to calcium oxide and carbon dioxide (when exposed to furnace temperatures of 1,0000C or more, limestone is calcined to quicklime.\| [0113] Treatment processes applied to this side stream may also incorporate steps to recover base metals and other valuable components in solution, including nickel, copper and iron, hi one form, side-stream treatment may involve adding an inexpensive alkali, e.g. calcined lime, dolomite, limestone or the like. Sulfate ions can be removed via the following equation (shown for normal ammonium sulphate and calcium oxide):(NILt)2SO4 + CaO + 3H2O -» CaSO4.2H2θΨ + 2NH4OH (10) ammonium quicklime gypsum ammonium\| [0114] Sulfate hydroxide\| [0115] In an embodiment the control mechanism 96 may be further arranged to add fresh ammonia to the circulating solution, at an appropriate rate, to account for any losses of ammonia.\| [0116] FURTHER DETAIL OF ABSORPTION/SCRUBBING CHAMBER OPERATION Conditions in the absorption chamber 28 may be strongly oxidising to assist the conversion of the impurity gases dissolving in the aqueous phase of the slurry (i.e. SOx ending up as sulfates rather than sulfites, and NOx ending up as nitrates rather than nitrites). In an embodiment, the cool, saturated condition of the flue gases when in the absorption chamber 28, plus the partial pressure of oxygen in these gases of three per cent or more, may be sufficient to ensure oxidising conditions. As well, the large pool of slurry held in the bottom of the absorption chamber 28 may be aerated using compressed air as is normal practice with flue gas desulfurisation (FGD). However, if additional oxidising is required, the process may further involve irradiation of the flue gases immediately upstream of their entry into the absorption chamber 28 by electron beams or high- voltage brush discharge, to form free radicals from water and oxygen (OH" and 0~). These are powerful oxidising agents, able to convert rapidly, sulfur dioxide SO2 to the trioxide SO3, and nitric oxide NO to the dioxide NO2, the precursors to sulfates and nitrates respectively. Thus, the absorption chamber 28 may serve as a highly efficient scrubber for the removal of SOx and NOx. It may also remove volatile metals that may exist in trace quantities in coal and that end up in flue gases notably mercury (the low operating temperatures and oxidising environment will tend to favour the conversion of any mercury vapour present to non- volatile mercuric oxide, an insoluble solid that will accompany the final product metal carbonate and silica to their permanent emplacement).\| [0117] FURTHER DETAIL OF PRESSURE EXCHANGERS\| [0118] With reference to Fig. 4, there is shown an arrangement for the pressure- exchange apparatus described above. At the end of the reaction process, the pressure ofthe final carbonate-rich product must be reduced from approximately 120 Bar to atmospheric pressure. Instead of merely reducing pressure by throttling valves, thereby losing the energy embodied in this pressure, the energy this pressure represents may be conserved by transferring it to the extent possible, to the silicate slurry. In Fig. 4, slurry A comprises the products of the reactions that occur as the ammoniated, carbonated silicate slurry flow through the pipeline 44 from the power station to the mine site; while slurry B represents silicate slurry from the mine. A consequence of pressure exchange in these two stages is that slurry A's pressure would fall from around 120 Bar to near ambient pressure, while that of slurry B would rise from around atmospheric pressure to perhaps 100 Bar.\| [0119] Another pressure-exchange apparatus is also utilised at the power station site. Here, using the terminology of Fig. 4, slurry A represents the hot silicate slurry arriving via the pipeline from the mine; while slurry B comprises slurry exiting the scrubbing chamber 30 (i.e. silicate slurry now charged with ammonia and carbon dioxide, but at close to ambient pressures). A consequence of pressure exchange in this stage is that slurry A's pressure would fall from its arrival pressure (this may be 120 Bar, a pressure that would be maintained by booster pumping stations at strategic locations along the pipeline 44 to overcome friction losses), to near ambient pressure. This pressure may be transferred (exchanged) to the extent possible to slurry B, thereby minimising the amount of pumping energy required to raise the pressure of this slurry to the levels required, here assumed to be 120 Bar. Since slurry A at this point will be at well below 120 Bar, pressure-exchange between slurries A and B alone may not be capable of raising the pressure of slurry B to 120 Bar. Also, the volume of slurry B may exceed that of slurry A. This is because of the much higher contents of carbon dioxide and ammonia, and of water condensed out of the power station flue gases. In an embodiment, additional pumping capacity may be installed to boost slurry B pressures to those required for the pipeline 44, and to pressurise those (relatively small) quantities of slurry B that cannot be pressurised by pressure-exchange with slurry A. For this function, conventional high-pressure diaphragm pumps, such as the Geho pump manufactured by Weir Netherlands b.v., may be implemented. This pumping, together with the pumping energy required to maintain pressures along the length of the pipelines, account for a substantial proportion of the total mechanical energy input to the total process. Other suitable pressure exchange/pump-turbine sets may comprisecentrifugal pumps and radial-type hydraulic turbines. As the pressures are relatively high, the type of centrifugal pump may be a multi-stage barrel-type pump.\| [0120] With reference to Fig. 5 there is shown a configuration for the heat exchanger arrangements 40 & 46, according to an embodiment of the present invention. As previously discussed, high temperatures are required to initiate and accelerate the carbon sequestration reactions: the conversion of metal silicates to carbonates. These reactions, being exothermic, yield additional heat that can and should be applied to assist with creating the conditions needed for these reactions to proceed most efficiently. As shown, the heat-exchanger arrangement is in the form of a simple shell- and-tube heat exchanger, consisting of two concentric pipes: the inner forms the "tube", the outer, the "shell". An advantage with this arrangement is that the heat exchanger can be made as long as is required to affect the desired transfer of heat: if necessary, many hundreds of metres long. For heat exchanger 40 (i.e. the heat exchanger on the silicate rock quarry site side), heat energy is transferred between the final carbonate/silica product (i.e. slurry A), which is hot, and the silicate slurry (slurry B), which is cool. For heat exchanger 46 (i.e. the heat exchanger on the power station side), slurry A would be hot silicate slurry from the quarry, while slurry B would be slurry exiting the scrubbing chamber 30 (i.e. now charged with ammonia and carbon dioxide, but at close to ambient temperatures).\| [0121] UNDERGROUND REACTOR\| [0122] Turning now to Fig. 2, there is shown an alternative system 200 for performing carbon dioxide sequestration which utilises (where geological conditions permit) an underground chamber as the reactor, as opposed to a pipeline reactor as illustrated in Fig. 1. In this embodiment, the reactor is in the form of a chamber 70 excavated from bedrock at a depth sufficient to allow the conditions for the core carbonation reactions to be generated entirely or partly by static head alone (e.g. 100 Bar). A chamber 70 excavated at a depth of approximately 800 meters and having a volume of 300,000 cubic meters, sufficient to allow for a 24 hours' detention time for the contents, may be envisaged for holding the reactive slurry output from a system 200 fitted to an efficient\| [0123] 1,000MWe coal-fired power station. In practice a smaller chamber may suffice, should it arise that the reactions are essentially completed in less time.\| [0124] The silicate slurry 36 may be prepared either at the serpentine quarry site andpumped overland to the power station site, or, the mineral could be railed, trucked or otherwise suitably transported to the power station site, and prepared there. Were the former implementation adopted, pipeline arrangements 44 would be considerably simpler than for the pipeline reactor embodiment described above with reference to Fig. 1. Specifically, the silicate slurry 36 would not be required to collect and transport heat and pressure energy from the quarry site to the power station site, nor to host any residual ammonium salts. The pipeline 44 would simply be utilised for mineral transport; whether it was transported as a lump product by rail or as slurry by pipeline would be determined by economic and environmental considerations. It will be appreciated that in this embodiment, silicate slurry density may be substantially higher (e.g. 60 per cent solids by weight), thereby reducing the volumes of silicate slurry required to be pumped, and allowing a lower pipeline velocity because of the reduced tendency for the solids in denser slurries to segregate and silt up the pipeline 44. Also, arrangements for conserving heat and pressure are much simpler than they would need to be for the pipeline reactor alternative.\| [0125] In Fig. 2, an injection pump 72 is utilised to drive the circulation of the reactive slurry from the scrubbing chamber 40, through a plurality of counter-current heat exchangers 74, 76, underground reactor 70 and counter-current decantation system for the separation of normal ammonium carbonate and other salts in the aqueous phase of the products of the underground reactor, and the insoluble carbonated mineral solids that are to be emplaced permanently.\| [0126] Heat exchangers 74, 76 are shown in schematic form at two locations on Fig. 2. The heat exchangers 74, 76 may be long, shell-and-tube designs, as shown in Fig. 4: they may span most of the vertical distance from the scrubbing chamber 40 down to the underground chamber 70. This is to say, whereas two separate pipelines are implied in Fig. 2, in practice, for most of their length they may be concentric: the annulus formed between the outer and concentric inner pipe transporting the hot reaction products, while the inner pipe transports the products heading downward to the Reaction chamber. It will be understood by persons skilled in the art that this selection may be reversed.\| [0127] In contrast to the pipeline reactor configuration shown in Fig. 2, heating of the reactive slurry may be accomplished by exchanging heat from the hot reaction productsrising first from the ammonia gas recovery vessel 78, and as the raw slurry descends further, from hot slurry rising from the underground chamber 70. While some supplementary heat may be required, the heat generated by Equation 2(b) would be conserved, and available to heat raw reactive slurry. The design of the underground chamber 70 may be optimised to achieve some plug- flow characteristics. In an embodiment, the chamber 70 may have a high length- to-diameter ratio of 10: 1 and be vertically aligned. Utilising a vertically aligned chamber provides that the incoming reactive slurry, being cooler hence slightly denser than the average contents of the reactive chamber 70, will tend to stratify at lower levels, displacing hotter slurry upwards. In an embodiment, the underground chamber 70 may be subdivided into two or more vertically stacked sub-chambers.\| [0128] In an embodiment, the reactive chamber 70 may employ an agitator (not shown) to maintain the solids in suspension. This may be advantageous where large residence times are required, implying in turn large reactor volumes. As will readily be appreciated, heat losses from the underground chamber 70 and pipelines may be much smaller than they would be even from a lagged above- ground pipeline and may be further reduced by insulation surrounding the reactor, pipelines and any other underground process vessels. Whereas an overland pipeline represents a plug-flow reactor, ideal conditions for a relatively slow series of reactions as are involved in carbon sequestration are also obtained in the embodiment illustrated in Fig. 2.\| [0129] It is noted that in the Fig 2 embodiment, the two overflow streams from the CCD system are handled separately. The overflow of the first thickener tank 90a is blended with the silicate slurry 36, incoming from the quarry site to form the circulating solution to be sent to the absorption chamber 28.\| [0130] The balance of the process in relation to sequestration, separation and emplacement is as for the overland pipeline reactor case.Example\| [0131] Again with specific reference to Fig. 3, a non-limiting example process flow for carbon sequestration for the first system configuration 10 described herein (i.e. the system depicted in Fig. 1) will now be given, wherein for convenience, like parts to those shown in the foregoing embodiment have been numbered with like numerals.\| [0132] Example 1\| [0133] Table 1: Indicative mass balance figures from 1.000 MWe of black coal-fired electricity generation plant. Material Per year Per hour\| [0134] Total CO2 generated: 6.4 m. tonnes 80O t\| [0135] (NKU)2CO3 to absorb 90% of this CO2 1,60O t\| [0136] Resulting quantity OfNH4HCO3 formed 2,400 1\| [0137] Water to make up 25% solution OfNH4HCO3 7,200 t Serpentine to absorb 90% of this CO2, 80% eff. 17.2 m tonnes 2,150 t\| [0138] Total slurry with NH4HCO3: 9,350 t\| [0139] Slurry density: 1.2 t/m3 1.2 t/m3\| [0140] Slurry volume, m3 8,000 m3\| [0141] Product (carbonate plus silica) solids: 20.6 m. tonnes 2,600 1 Slurry pipe dia. with 3 m/s velocity: 1.0 metres 1.0 metres\| [0142] Ammonia lost due to SOx (90% recovery via Eq. 10) ) 11,,66000O 1t 0.2 t\| [0143] Ammonia lost due to NOx 3,0001 0.37 t\| [0144] Total losses of ammonia: 4.600 1 0.57 t\| [0145] Table 1 provides an indicative detailed mass balance for a carbon dioxide sequestration process, assuming:\| [0146] - 90 per cent carbon dioxide capture and sequestration from 1,000 MWe of black coal- fired electricity generation plant, which when operating in base-load mode might expect to generate annually 8,000 GWh of electricity; - where on a dry ash-free basis, the coal is 81.3% by weight carbon and 0.65% sulphur (as S) and the flue gases contain 400 ppm NOx.An advantage of the carbon dioxide sequestration process 100 and systems 10, 20 according to embodiments of the present invention is that by selecting ammonia as a catalyst/promoter, a single integrated process can be provided for both capture and sequestration of carbon dioxide. In an embodiment, sequestration of the carbon dioxide takes place in a reactor, in the form of a return pathway 52 of a pipeline 44, which advantageously connects the power station (i.e. the source of carbon dioxide) to the source/destination of the absorbent material being used in the process, hi an alternative embodiment, where geological conditions permit, the reactor may take the form of an underground chamber which advantageously facilitates the reaction without requiring pressure-exchange and head-recovery equipment required for the pipeline embodiment. Another advantage of the carbon dioxide sequestration process and systems is that the reaction kinetics may be improved by using ammonia. Therefore, by using ammonia and exploiting the heat generated by the exothermic reaction, the energy consumption of the process 100 can be kept to a minimum. As the reaction products are thermodynamically stable, carbon dioxide can be stored in a permanent stable solid form. Following from this, further advantages include lower operating and capital costs.\| [0147] Persons skilled in the art will appreciate that further advantages may arise from carrying out certain steps of the aforementioned embodiments in isolation. For example, the catalytic effect of a solution of ammonia with an ammonium salt (that may be ammonium carbonate formed by exposing an ammonia-rich solution to a gas stream containing carbon dioxide) in the carbon dioxide sequestration process can also be utilised for extracting metals (e.g. magnesium, iron, nickel, copper and other metals present in the silicate rock) from metal silicates, such as magnesium-rich metal silicates. In such an embodiment a solution of ammonia-rich ammonium carbonates in water may be mixed with a metal silicate (typically in slurry form) to allow the dissolution of magnesium ions by ammonia to recover the metal, in this embodiment a metal compound in the form of magnesium carbonate. The mixing may occur in an ammonia absorption chamber such as that previously described in connection with the preceding embodiments. Preferably the solution contains molecular ammonia in the presence of ammonium salts in solution, such as ammonium carbonate, to prevent the precipitation of magnesium hydroxide, hence allowing the dissolution of magnesium ions by ammonia to continue, substantially free of concerns over tendencies for otherwiseinsoluble magnesium hydroxide to coat, and restrict access to the silicate mineral by carbon dioxide and ammonia. A further advantage arising from this process is that after extraction of magnesium carbonate, other minerals (metals) present within the silicate rock are also amenable to recovery. The silicate rock may comprise mafic or ultra- mafic rocks (i.e. rocks with respectively a high or very high ratio of magnesium to silicon content).\| [0148] Expressed another way, the catalytic effect of the ammonia follows from its tendency to form complexes (ammines) with certain metal ions including magnesium (Mg2+), divalent iron (Fe2+), copper (Cu2+) and nickel (Ni2+). The presence of ammonium salts notably the various carbonates formed from the reaction between ammonia and carbon dioxide prevents precipitation of the otherwise insoluble magnesium hydroxide. Magnesium carbonate is however insoluble in such an environment, so a precipitate of this compound will form from the reaction between magnesium hydroxide and ammonium carbonate, to yield ammonium hydroxide and free molecular ammonia in solution, the latter continuing to extract additional magnesium and other metals from the silicate rock through formation of ammine complexes until all such susceptible metals have been extracted.\| [0149] Finally, it is to be appreciated that various alterations or additions may be made to the parts previously described without departing from the spirit or ambit of the present invention. The process is not limited to having a single two-stage continuous reactor, or a single tube-like reactor, as the process may be arranged to utilise alternatively configured items of equipment as necessary to accommodate process variables, arising from different source materials, capital and operating costs. For example, in the exemplary embodiment previously described the plant design is based on the emission of 800 tonnes CO2/GWh generated from a state-of-the-art black coal- fired electricity generation plant. By comparison, the Bayswater Power Station and the Liddell Power Station, both in the Hunter Valley of New South Wales, Australia, able to generate 2,640 MWe and 2,040 MWe respectively, being older hence less efficient can be expected to emit between 850 and 900 tonnes CO2/GWh. Thus the concentration and rate of carbon dioxide emissions in the flue gas emitted by the power plant may vary such that the plant equipment design may be reconfigured to accommodate these variables. For example, alternative equipment can be configured for the various heat and pressure exchange stations. The carbon dioxideabsorption zone and the scrubbing zone may be arranged in series in two separate vessels (rather than the nested configuration shown in Fig. 1). The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s). As well, the corresponding solids concentration in the slurry feed may be higher or lower than 25% solids by weight. It is possible that the metal silicate solution may comprise a blend of metal silicates, e.g. mixture of serpentines and olivines, even pyroxenes. The reaction kinetics may require heat to be removed from the reactive solution (rather than heat addition as described above). These factors will impact and alter the system pressures. There might be two or more pipelines for transporting the metal silicate solution and the reactive solution; because there are more pipelines, additional heat exchangers and pressure-exchange apparatus may be used. The power station flue gas may include additional pre-processing steps including flue gas desulphurisation (FGD) and selective catalytic reduction (SCR) to reduce concentrations of SOx and NOx respectively hence losses of ammonia from the system. Furthermore, the availability of services, such as steam and cooling water may require different equipment arrangements.\| [0150] Any reference to prior art contained herein is not to be taken as an admission that the information is common general knowledge, unless otherwise indicated.\| [0151] In the claims which follow and in the preceding description of the invention, except where the context requires otherwise due to express language or necessary implication, the word "comprise" or variations such as "comprises" or "comprising" is used in an inclusive sense, i.e. to specify the presence of the stated features but not to preclude the presence or addition of further features in various embodiments of the invention.	(WO2010/088738)\|[0001] SYSTEM, APPARATUS AND METHOD FOR CARBON DIOXIDE\| [0002] SEQUESTRATION\| [0003] Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\| [0004] Background to the Invention\| [0005] There is increased focus on reducing carbon dioxide emissions to the atmosphere, to help minimise the effects of global warming. Carbon dioxide sinks exist naturally, with the main naturally occurring sink being the ocean. Plants are also an effective form of carbon dioxide sink and use photosynthesis to remove carbon from the atmosphere by incorporating it into biomass. However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\| [0006] A major source of harmful carbon dioxide gases are large fossil fuel power stations which, when fuelled by black coal, on average typically output around 0.8 to one tonne of the gas for each MegaWatt-hour (MWh) of electricity they generate. For example, a large power station such as the 2,640 MW Bayswater in the Hunter Valley of New South Wales, Australia, in generating 20 million MWh of electricity in a year, would also output 18 million tonnes of carbon dioxide. It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations. It would also be advantageous if a system and method were provided for the disposition of the gas to be independently audited in perpetuity.\| [0007] Summary of the Invention hi a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| [0008] (i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium carbonate that is able to absorb the carbon dioxide, whereby thecarbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate;\| [0009] (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| [0010] In the context of the present specification, the phrase "solution rich in normal ammonium carbonate " will be understood as referring to a solution whereby the main salt present corresponds to the formula for the normal form of ammonium carbonate\| [0011] (NILO2CO3.. There solution may, however, consist of other ammonium carbonate salts, and there may also be some molecular ammonia NH3, and ammonium hydroxide NH4OH, also present. Further, it should be noted that the terminology "gas stream containing carbon dioxide" does not mean that the stream contains only carbon dioxide, and may contain other off gases.\| [0012] hi an embodiment the metal silicate rock is mixed with the normal ammonium carbonate solution prior to absorbing the carbon dioxide in step (i).\| [0013] hi an embodiment the reaction causes the bicarbonate in the presence of the metal silicate to partially decompose so as to produce an aqueous phase enriched in molecular ammonia and carbon dioxide.\| [0014] hi an embodiment the method comprises the further step of cooling the aqueous phase such that free ammonia and carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered for re-use in step (i) of the process.\| [0015] hi an embodiment the method comprises the further step of adding an alkali to the recovered ammonium carbonate in solution prior to being re-used in step (i). The alkali may be calcium oxide and/or hydroxide, hi an embodiment the calcium oxide is extracted from gas stream prior to scrubbing in step (i).In an embodiment the method comprises the further step of introducing pulverised limestone into a source producing the carbon-dioxide rich gasses. The source may be a coal-fired power station boiler and the pulverised limestone is added upstream of an economiser section of the power station boiler.\| [0016] In an embodiment a portion of the mixed solution used to scrub the gas stream prior to discharge to the atmosphere is chilled to ensure that a quantity of free ammonia in the gases is below a threshold level. The threshold level may, for example, be set by the relevant government or other regulatory body.\| [0017] In an embodiment the step of scrubbing the gas stream comprises exposing the carbon dioxide-containing gas stream to the slurry as a spray or deluge operable to maximise the area of exposure between the slurry and the carbon dioxide-containing gas.\| [0018] In an embodiment the step of controlling the reactor comprises elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\| [0019] In an embodiment the reactor is a pipeline. The pipeline may comprise multiple flow paths and wherein the reaction takes place along the length of one of the flow paths. Another of the flow paths is utilised to supply the metal silicate slurry to the first stage.\| [0020] In an embodiment the method comprises the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\| [0021] In an embodiment the reactor is a chamber located in use underground. The chamber may be located at a depth that provides sufficient pressure by way of static head to enhance the reaction between the carbon dioxide and the metal silicate.In an embodiment the method comprises the further step of grinding a metal silicate rock to produce the metal silicate slurry. The metal silicate slurry may comprise roughly 25% by weight finely ground metal silicate solids.\| [0022] In an embodiment the metal silicate is a magnesium-rich silicate. In an embodiment the magnesium rich silicate is a serpentine and/or olivine and/or pyroxene mineral all commonly described as ultrabasic or ultramafic minerals.\| [0023] In an embodiment the method comprises the further step of cooling the normal ammonium carbonate-metal silicate slurry prior to it use in scrubbing carbon dioxide from flue gases.\| [0024] In accordance with a second aspect of the present invention there is provided a system for sequestering carbon dioxide from a gas stream, the system comprising: (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and\| [0025] (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\| [0026] In an embodiment the first apparatus comprises an absorption chamber arranged to circulate the normal ammonium carbonate solution through the carbon dioxide to thereby absorb the carbon dioxide.\| [0027] hi an embodiment the reactor is the pipeline as used in the method according to the first aspect.\| [0028] In an embodiment the reactor is the chamber used in the method according to the first aspect.In an embodiment the reaction of the bicarbonate with the metal silicate further produces an aqueous phase containing molecular ammonia, carbon dioxide and water.\| [0029] In an embodiment the system further comprises a cooling arrangement arranged to cool the aqueous phase such that free ammonia and remaining carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered by a recovery arrangement for reuse by the first apparatus.\| [0030] In an embodiment the system further comprises a separation system arranged to separate the recovered ammonium carbonate in solution from the insoluble metal carbonate-silica phase prior to recovery. The separation arrangement may, for example, be a counter-current decantation (CCD) system comprising one or more stages for separating the solution.\| [0031] In an embodiment the system further comprises a control arrangement arranged to add an alkali to the recovered ammonium carbonate in solution prior to returning it to the first apparatus for re-use.\| [0032] In an embodiment the alkali is calcium oxide and/or hydroxide. The calcium oxide is extracted along with other suspended solids (fly ash solids) from the gas stream prior to scrubbing.\| [0033] In an embodiment the system further comprises a feeder arranged to feed pulverised limestone into a source producing the carbon-dioxide rich flue gases. The point source may, for example, be a coal-fired power station and the pulverised limestone is fed into raw flue gases upstream of the power station boiler's economiser.\| [0034] In an embodiment the metal silicate comprises a magnesium rich silicate as used in the method according to the first aspect.In an embodiment the system further comprises an ammonium carbonate salt recovery arrangement arranged to recover ammonia and ammonium salts accompanying the final product.\| [0035] In an embodiment, the system comprises a solids-liquids separation system arranged to separate and recover ammonium carbonate salts, from the metal carbonate solid product that is sent for final emplacement.\| [0036] hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica.\| [0037] In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\| [0038] In an embodiment the slurry provided to the chamber is the reactive slurry produced in the process of the first aspect.\| [0039] In an embodiment the method comprises the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber.\| [0040] In an embodiment the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.In accordance with a fifth aspect there is provided a power station or other point source of carbon dioxide-rich flue gases, such as a blast furnace as used in steel making, or a cement kiln, utilising a carbon sequestration system in accordance with the second aspect, the system arranged to capture and sequester carbon dioxide from flue gas emitted by the power station or other point source.\| [0041] In accordance with a sixth aspect, in an ammonia absorption process in which a metal silicate rock is mixed with a normal ammonium carbonate salt solution in water so as to produce a normal ammonium carbonate salt solution in water/metal silicate slurry (the ammoniated slurry) for use in a carbon dioxide sequestration process, there is provided the step of chilling the ammoniated slurry to limit losses of ammonia in scrubbed flue gases to the extent necessary to meet emission limits applying at the location in question.\| [0042] hi an embodiment, the process comprises the further step of providing the ammoniated slurry to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammoniated slurry to thereby absorb the carbon dioxide into a reactive slurry.\| [0043] In accordance with a seventh aspect of the present invention there is provided a method of extracting a target metal from a metal silicate comprising the step of mixing the metal silicate with an ammonia-rich ammonium carbonate salt solution, and reacting the mixed solution to cause the target metal to dissolve into the solution.\| [0044] In an embodiment the method comprises the further step of grinding the metal silicate and forming it into a slurry prior to mixing the metal silicate with the solution.\| [0045] In an embodiment the metal silicate is a magnesium-rich silicate.\| [0046] hi an embodiment the magnesium-rich silicate is a serpentine and/or olivine and/or pyroxene silicate mineral commonly described as an ultrabasic or ultramafic mineral.In an embodiment the solution comprises normal ammonium carbonate salts dissolved in water (the ammoniated solution).\| [0047] In an embodiment the target metal dissolves into the solution and then precipitates in the presence of carbon dioxide, as a metal carbonate to be removed for recovery.\| [0048] In an embodiment the target metal is one or more of magnesium, calcium or iron. The dominant metal within the metal silicate may comprise magnesium.\| [0049] In an eighth aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| [0050] (i) in a first stage, mixing a slurry of a metal silicate rock with a normal ammonium carbonate solution so as to produce a normal ammonium carbonate salt/water/metal silicate slurry;\| [0051] (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the chilled solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| [0052] (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\| [0053] Brief Description of the Drawings\| [0054] An embodiment of the present invention will now be described, by way of example only, with reference to the accompanying drawings, in which:\| [0055] Fig. 1 is a schematic of a carbon dioxide sequestration system according to an embodiment of the present invention;\| [0056] Fig. 2 is a schematic of a carbon dioxide sequestration system according to an alternative embodiment of the present invention;\| [0057] Fig. 3 is a process flow diagram showing a method of sequestering carbondioxide using the system of either Fig. IA or IB, in accordance with an embodiment of the present invention;\| [0058] Fig. 4 is a schematic of a heat exchange apparatus, in accordance with an embodiment of the present invention;\| [0059] Fig. 5 is a schematic of a pressure exchange apparatus in accordance with an embodiment of the present invention; and\| [0060] Fig. 6 is a schematic illustrating a metal silicate preparation and grinding technique, in accordance with an embodiment of the present invention.\| [0061] Detailed Description of an Embodiment\| [0062] In the following description, embodiments of the present invention are described in the context of a system, apparatus and method for the capture and sequestration of carbon dioxide contained within flue gases emitted by a fossil fuel-fired power station. However, it is to be understood that the system, apparatus and method could equally be utilised for the permanent sequestration of carbon dioxide from any 'point' source and is not limited to the particular arrangement described herein. With reference to Fig. 1 there is shown a flow diagram of a system 10 for performing a carbon dioxide (CO2) sequestration process from a gas feed stream containing carbon dioxide outputted from a power station, in accordance with a first embodiment of the present invention. With additional reference to Fig. 3, the system 10 is arranged to perform the process 100 of (i) scrubbing a gas stream containing carbon dioxide with a normal ammonium carbonate solution that is able to absorb the carbon dioxide, whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising, in the main, ammonium bicarbonate; and (ii) passing a slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| [0063] In an embodiment the method may further comprise a stage (iii) of contacting flue gases with a circulating dilute normal ammonium carbonate solution that may be chilled to the extent necessary, in a vessel in a counter-current, staged manner so thatresidual ammonia in the flue gases is scrubbed from these gases to levels low enough to allow their final discharge in the atmosphere.\| [0064] In the illustrated embodiment the stages (i) and (iii) are performed within a first apparatus 20 having separate chambers, in the form of an absorption chamber 28 and a scrubbing chamber 30, respectively. Stage (ii) occurs within a reactor either in the form of a pipeline 52 (as shown in Fig. 1) or, as will be described in more detail in subsequent paragraphs with reference to Fig. 2, an underground chamber excavated at a sufficient depth to facilitate conditions for the carbonation reactions to take place. According to Fig. 1, the pipeline 52 may connect the reactor to a mineral quarry site from with metal silicate is sourced.\| [0065] The carbon dioxide sequestration process utilised in embodiments of the present invention is based on mineral carbonation. Mineral carbonation is a reaction between a metal-oxide-bearing mineral material and carbon dioxide. The metal-oxide bearing material may, for example, be alkaline-earth metals. Advantageously, the process 100 does not require the source of carbon dioxide to be particularly pure. In mineral carbonation, carbon dioxide reacts with the metal oxide bearing material to generate insoluble carbonates, that is to say:\| [0066] MO + CO2 → MCO3 + heat (1)\| [0067] which is an exothermic reaction, occurring more rapidly at elevated temperature, typically above 1500C. Certain chemicals may serve to increase the rate at which this reaction proceeds without being consumed themselves, i.e. they serve as catalysts. The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage). Further, embodiments are inherently operable to make bicarbonate ions as carbon dioxide is absorbed into the ammonia-rich ammonium carbonate solution, without having to handle highly pressurized carbon dioxide.\| [0068] The exact nature of the insoluble carbonates formed by the reaction depends on the metal-oxide bearing material. Suitable materials may be naturally occurring alkaline-earth metal-rich silicate rocks which contain mineral constituents such asserpentine (Mg3Si2O5(OH)4), olivine (Mg2SiO4), orthopyroxene (MgSiO3), talc (Mg3Si4O10(OH)2) and wollastonite (CaSiO3). In practice, the element Iron (Fe) may substitute for some of the Magnesium (Mg) or Calcium (Ca). Other suitable materials include alkaline industry residues such as slag from steel production, the ash (both fly and bottom) from pulverised coal-fired boilers, the ash remaining from the combustion of paper recycling residues (de-inking ash), and cement. The amount of heat generated in the reaction will depend on the specific metal and on the mineral containing the metal oxide as can be seen below in the case of three natural silicates (heat values are given per unit mole of CO2 and at standard conditions (25°C and 0.1 MPa):\| [0069] Olivine\| [0070] Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 + 89 kJ moll CO2 (2a)\| [0071] Serpentine Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol" 1 CO2 (2b)\| [0072] Wollastonite\| [0073] CaSiO3 + CO2 → CaCO3 + SiO2 + 90 kJ mol l CO2 (2c)\| [0074] In the illustrated embodiments, the silicate rock comprises the mineral serpentine, Mg3Si2O5(OH)4. AU of the above minerals may be pre-treated to increase the surface area of rock that can subsequently come into direct contact with the carbon dioxide. In an embodiment, the pre-treatment involves crushing, grinding and/or milling of the mineral, as well as some mechanical classification and separation. For example, the minerals could be milled (e.g. wet-milled) in ball mills or equivalent to form a finely ground metal silicate slurry (hereafter 'silicate slurry') 36 wherein 90% of the mineral matter is finer than 40 microns. However, it will be understood that the extent of the pre-treatment is dependent upon the source and type of mineral(s) being used in the process. An example milling and transportation process flow is shown in Fig. 6.\| [0075] Again with specific reference to Fig. 1, the carbon dioxide sequestration system 10 will now be described in detail. The system 10 receives a raw flue gas mixture feed stream 32 that has been generated and subsequently emitted by a powerstation or other point source (not shown). In the embodiment described herein, the raw flue gas mixture 32 is passed though a filter 33 to remove most of the particulate matter. Suitable filters may include fabric filters, electrostatic precipitators and the like. Cleaning the raw flue gas mixture 32 may serve to minimise both the maintenance costs in downstream gas-handling equipment and the concentrations of particulates in flue gases ultimately discharged to the atmosphere. It will be understood, however, that while desirable for process reasons, it is not essential that the raw flue gas mixture 32 be cleaned of all particulates before it enters the scrubbing chamber 30. In an embodiment, the filtering process may additionally involve controlling the level of SOx and NOx that is present within the flue gas so as to adjust the pH level of the ammoniated slurry by virtue of the concentration of sulfate and nitrate ions present in it (which in turn affects the reaction rate between the silicate rocks and carbon dioxide by driving magnesium and calcium ions into solution) as will be described in detail below.\| [0076] To maximise heat recovery in the system 10, the filtered flue gas mixture is then passed through a heat exchange apparatus in the form of a heat exchanger 34 so that the sensible heat of the filtered flue gas mixture (typically at a temperature of around 135°C) is exchanged with the cooler gasses being expelled from the scrubbing chamber 30 of the first apparatus 20 and the filtered flue gas mixture is cooled to its water-vapour saturation temperature (i.e. to about 50°C). Suitable heat exchangers may include, for example, recuperative-type heat exchangers, such as the Ljungstrom rotary design as commonly used for air pre-heating in power stations.\| [0077] As mentioned in preceding paragraphs, the carbon dioxide sequestration system 10 receives a source of silicate slurry 36. According to the embodiment described herein, the silicate slurry source is located near or at the mine site from which the silicate rocks are sourced. As previously described, the silicate mineral sourced from the mine site is finely ground (e.g. by wet-milling in ball mills or equivalent to form the slurry) wherein roughly 90% of the mineral matter is finer than 40 microns or as determined to be appropriate for the proper operation of the process.\| [0078] According to Fig. 1, the silicate slurry 36 is first blended with a solution in water of normal ammonium carbonate to create an ammonia rich ammonium carbonate- metal silicate slurry (hereafter "absorbent slurry"). In the illustrated embodiment, the normal ammonium carbonate salts in solution (hereafter "circulating solution") is the solution in water of most of the normal ammonium carbonate salts accompanying thefinal metal carbonate/silica product. Specifically, according to the Fig. 1 embodiment, the circulating solution represents the overflow of a first thickener 90a of a counter- current decantation (CCD) thickener separation system 90.\| [0079] In flowing from the CCD thickener system 90 to the power station site, the absorbent slurry 47 passes through a first pressure-exchange apparatus 38. To minimise power consumption, the pressure of the absorbent slurry 47 may be increased by exchanging pressure with the final metal carbonate/silica product (hereafter 'final product'), typically to a pressure of approximately 100 Bar. hi addition, to minimise heat losses from the system 10 (and to ensure that the final product is cooled to a suitable temperature before it is emplaced in its final permanent repository), the absorbent slurry 47 passes counter-currently through a heat exchanger 40 to absorb the surplus sensible heat contained in the final product.\| [0080] According to Fig. 1, a pipeline 44 connects the first apparatus 20 to the silicate mineral quarry site and is used to transport the absorbent slurry 47 used in the sequestration process 100. As will be described in more detail in subsequent paragraphs, an alternate path 52 in the pipeline 44, in this embodiment, also serves to act as a controlled reactor in which the metal carbonation reaction largely takes place. At or near to the power station site, the absorbent slurry 47 is passed counter-currently through a second heat exchanger 46 and a second pressure-exchange apparatus 48, where the absorbent slurry 47 is cooled and reduced in pressure by exchange with the reactive slurry discharged from the first apparatus 20, before being fed directly into the scrubbing chamber 30.\| [0081] After arriving at the power station site, a residual circulating stream passes into a vessel in the form of a residual ammonia scrubber 56, in such a way that flue gases that have been stripped of most of their carbon dioxide content, pass upwards from below. There may be any number of counter-current contacting stages, depending only on the desired implementation. The residual ammonia scrubber 56 is operable such that the cleaned, largely carbon dioxide-free flue gases may leave the system with less than one part per million of ammonia, hi order to achieve such low losses of ammonia, the fluid circulating through this vessel may be cooled, even chilled, to an appropriate degree. Specifically, the fluid circulating through this vessel is comprised of the dilute aqueous phase described above (i.e. a clarified, dilute solution in water of normal ammonium carbonate), which enters the vessel and collects in the base of the residualammonia scrubber 56 from where it is circulated by pumps to the header sprays to above the uppermost of the contacting stages. It is this circulating flow that is cooled to the requisite extent, by firstly, arranging for it to flow firstly, through one or more first stage heat exchangers that are cooled by circulating water cooled in turn, in a cooling tower, and secondly, through one or more second-stage heat exchangers that are cooled in turn, by a stream of water or other suitable heat-exchange fluid that has been chilled to below ambient temperatures by a chilling plant suitable for the purpose. In an embodiment, the chilling plant is an ammonia absorption chiller 82, the operating principles of which are understood by those skilled in the appropriate art. It is to be understood however, that alternative types of chilling plant provided they have adequate chilling capacity, are equally suitable.\| [0082] Absorption chillers, including ammonia absorption chillers, require a source of heat for their operation. In an embodiment, some of this heat may be provided by the heat released through carbonation reactions as shown as equations 2a, 2b and 2c, depending on the type of silicate mineral used.\| [0083] The cooled filtered flue gas mixture passing through the heat exchanger 34 enters the scrubbing chamber 30 where the gas mixture passes upwards through deluging sprays of circulating solution entering from the residual ammonia scrubber 56 from above. When carbon dioxide is absorbed in the circulating solution, a further substantial quantity of heat is liberated, as gaseous carbon dioxide is absorbed into it, and reacts with the normal ammonium carbonate salts in the circulating solution. The reactions include the conversion of the normal ammonium carbonate (NELt)2CO3 to the bicarbonate NH4HCO3, via the reaction:\| [0084] (NFLt)2CO3 + CO2 + H2O -» 2NH4HCO3 (3)\| [0085] Normal ammonium Ammonium\| [0086] Carbonate bicarbonate\| [0087] While this will be the main reaction encountered, other reactions may equally occur in parallel including, when there is free molecular ammonia present in the scrubbing solution:\| [0088] NH3 + CO2 + H2O -> NH4HCO3 (3a)As well, some of the ammonium bicarbonate may lose some combined water to form the carbamate, NH2COONH4, hence this compound will likely be present in smaller quantities, perhaps along with some urea, CO(NH2)2, formed when the carbamate loses additional combined water.\| [0089] FURTHER DETAIL OF SEQUESTRATION PROCESS\| [0090] In more detail, the carbon capture process begins with the metal silicate (in this case, ground serpentine) being blended into a circulating solution of serpentine and an aqueous phase containing normal ammonium carbonate in solution to thereby produce the absorbent slurry. The absorbent slurry is then circulated using pumps, through a carbon dioxide absorption chamber 28 which in an embodiment may be the lower half of a tall scrubbing chamber 30 (the upper part being utilised as the residual ammonia scrubber 56). The absorption chamber 28 may, for example, take the form of a flue gas desulfurization scrubber, with the absorbent slurry circulated at high flow rates through banks of sprays.\| [0091] The absorbent slurry is heated by the transfer of latent heat from the flue gases rising from below. Also, as mentioned above, when carbon dioxide gas is absorbed into the absorbent slurry, substantial quantities of heat are liberated, as carbon dioxide reacts with the mainly normal ammonium carbonate (NHi)2CO3, to form the bicarbonate NH4HCO3, as per Equation 3 (there may also be some intermediate salts e.g. the sesquicarbonate (NFLO2CO3. NH4HCO3, the carbamate NH4COONH2, and traces of urea, CO(NH2)2). The heat of solution, along with the latent heat released when water vapour in the flue gases condenses, is removed by circulating the absorbent slurry through water-cooled heat exchangers 84.\| [0092] As mentioned above, the output from the absorption chamber 28 is a reactive solution in the form of a metal silicate slurry in an aqueous phase that is itself a solution of carbonate-rich ammonium carbonates, primarily ammonium bicarbonate. A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor.On route to the mine site, at or near to the power station, the reactive slurry is pressurised at the second pressure-exchange apparatus 48 to a high pressure of around 120 Bar (above the critical pressures of both carbon dioxide and ammonia) and also heated to at least 100°C and preferably to at least 150°C. Heating is accomplished by transferring heat from the incoming silicate slurry arriving from the mine at the heat exchanger 46, and also, if necessary, by injection of steam 54. The heat contained in the incoming silicate slurry in part originates from reactions 2(a), 2(b), and 2(c), depending on the silicate mineral involved. hi the return pipeline 52 of the pipe reactor, at temperatures below 50°C or thereabouts, most if not all of the carbon dioxide present is in the form of ammonium carbonates. When the slurry is heated to at least 100°C under pressures of at least 100 Bar, the tendency is for the various forms of ammonium carbonates in solution to decompose to molecular carbon dioxide CO2 and ammonia NH3. These remain substantially in solution in the reactive slurry under these temperature and pressure conditions. A result of this process is the partial pressure of the carbon dioxide will be particularly high, thereby serving to enhance the speed of reaction with the silicate minerals, converting them to insoluble carbonates and silica during the transit. In an embodiment, the pipeline may be 10 kilometres in length to allow adequate time for the reactions to proceed essentially to completion resulting in the metal carbonate product that contained most if not all of the carbon dioxide originally scrubbed from the power station flue gases. It will be understood that the length may vary, however, depending on the actual implementation.\| [0093] It will be apparent that a high concentration of ammonia is maintained in the slurry throughout its passage from the power station to the silicate rock mine/quarry or other emplacement site.\| [0094] When the final product in the return pipeline 52 reaches the vicinity of the mine site, as described above, the hot pressurised final product transfers its sensible heat via the heat exchanger 40 to the absorbent slurry being pumped towards the power station, hi the process the final product is cooled to a temperature below 50°C. To achieve this temperature in practice, it may be necessary to employ additional cooling to ensure that the temperature of the final product stream is cool enough for the recombination reactions to occur. In an embodiment, the additional cooling is accomplished by means of a heat exchanger cooled by circulating cooling water fromdry (e.g. radiator-type) cooling towers, fin fan coolers, or a natural-draft cooling tower (not shown) such as used for cooling in the power station. A consequence is that free molecular ammonia and carbon dioxide will subsequently re-combine to form ammonium carbonate salts dissolved in the aqueous phase that can be recovered and used in the circulating solution. Since carbon dioxide has been removed from the aqueous phase by reaction with the mineral silicate, the ratio of carbon dioxide to ammonia is lower than it was before the key carbonation reactions occurred. Hence, the predominant form of ammonium carbonate salt formed is normal ammonium carbonate (NKU)2CO3 which, it will be noted, may contain twice as many ammonia units pre carbon dioxide unit as the bicarbonate, NH4HCO3. This is the reason why a solution rich in normal ammonium carbonate may also be referred to as an ammonia-rich ammonium carbonate solution. In any case, it will be understood that other ammonium salts, plus molecular ammonia NH3 and ammonium hydroxide NH4OH, may also be present.\| [0095] FURTHER DETAIL OF SEPARATION SYSTEM\| [0096] As previously mentioned, the final reacted slurry (i.e. containing mainly normal ammonium carbonate in solution together with the carbonate/silica solids that are the products of carbonation) is passed through a solids-liquids separation process. The separation process generally involves producing a clear overflow solution containing most of the ammonium salts and other soluble chemicals (including any molecular ammonia and ammonium hydroxide NH4OH that are dissolved in it) and a dense slurry or even paste-consistency underflow containing all of the solids.\| [0097] Separation may be accomplished by one or more of several means known to those skilled in the art. In an embodiment, a filtration process may be employed using, for example, rotary vacuum filters. In an alternative embodiment, the filtration process may use plate and frame-type filter presses. In both embodiments, a filter cake is formed on a filtration medium (a filter cloth for example) and wash-water is sprayed onto, or otherwise caused to pass through, the filter cake to wash out residual quantities of soluble materials including ammonium carbonate salts. The filter cake represents the first, solids-rich stream, which may be handled as a cake, or converted to a dense slurry by addition of small quantities of additional water sufficient to allow it to be handled asa slurry. The aqueous phase, including wash-water passing through the filter cake and filtration medium, represents the second stream. In another embodiment, separation of the solids from the aqueous phase (specifically, the separation of the ammonium carbonate salts and other soluble materials in the aqueous phase) is achieved by a process known as counter-current decantation (CCD), as illustrated in the Fig. 1 and 2 embodiments. This technique involves utilising a number of continuous thickener tanks (in the illustrated embodiment three tanks are used, although it will be understood by persons skilled in the art that more or less thickener tanks may be employed depending on the desired implementation) that are arranged in a series. The CCD thickener system 90 may recover a substantial amount (e.g. around 99 per cent) of all of the dissolved salts and other soluble substances (including ammonia) in the aqueous phase accompanying the final product. The remaining amount of salts will accompany the final product solids as they are pumped to their final permanent repository.\| [0098] It is noted that in some implementations, only a certain percentage (e.g. 80%) of soluble substances may be recovered by the first thickener 90a of the CCD system 90, with the remainder recovered by subsequent stages. In an embodiment, as shown in Figure 1, the two aqueous-phase streams resulting from the overflows of the first-stage and second-stage thickeners are blended either by arranging for the overflow of the second stage thickener to be blended with the feed stream to the first-stage thickener, or by directly blending the two overflow streams.\| [0099] In more detail, the final products stream from the reactor, after pressure reduction in the pressure exchangers 38 and cooling in the heat exchangers 40, enters the first thickener 90a of the series. The insoluble solids (the carbonated mineral) suspended in the feed stream settle in the thickener tank 90a to form a dense slurry that is withdrawn as an underflow stream. The balance of the feed entering the thickener tank overflows as a clarified supernatant, which contains most of the soluble ammonium carbonate salts and other soluble materials (i.e. the circulating solution). The underflow may still contain around 10 per cent of the aqueous phase that first entered the thickener, and it is the function of the balance of thickeners in the CCD system to recover these salts to the maximum practicable extent, from the insoluble solids that are to be finally emplaced. In the CCD system 90, the underflow slurry from thickener tank 90a is pumped to the next thickener tank 90b in line. Also fed to tank 90b is the clarified overflow from thickener tank 90c, and so on. Where "N" thickenertanks are employed, the final thickener tank in the series, tank N, receives a feed stream which is a mixture of the underflow of thickener tank N-I, and fresh water, which may be replaced in part by any surplus aqueous phase recovered from final emplacements of carbonated mineral as this further consolidates and/or drains from the mineral, over time. In an embodiment, a mixture of thickener tanks, one or more stages in series, and filtration units may be used to effect the separation of soluble ammonium carbonate salts from the insoluble carbonated mineral.\| [0100] The dense slurry stream (in one embodiment a filter cake, in another embodiment the underflow of CCD thickener Unit N) is the final product slurry substantially free of salts, and in a form suitable for permanent emplacement in mine voids or other purpose-built repositories (not shown). In these emplacements the solids can settle and consolidate, releasing additional aqueous phase as a clear supernatant. This supernatant may also be collected and re-used in the process, as described in the paragraph above. When the CCD system 90 for the recovery of ammonium salts is close to the power station, as may be the case for the underground chamber reactor embodiment (Fig. 2), it may be appropriate to add the remainder of the power station fly ash to the final product slurry from the carbon sequestration process, so the two streams may be handled and co-disposed of as a single stream. An advantage stemming from the presence of fly ash having pozzolanic properties (a tendency to "set" in the presence of alkalis and moisture) in the final product, is that it will assist with the rehabilitation process, by encouraging the final product/fly ash mix to "set", thereby immobilising the contents of the emplacement. hi an embodiment the overflow of the second stage of the CCD thickener system 90, being a relatively dilute, clarified (insoluble solids- free) solution in water of ammonia-rich ammonium carbonate salts may be handled separately (see Fig. 2). hi such an embodiment, the stream (hereafter "residual stream") is sent overland from the CCD system 90 (installed near the silicate quarry) to the power station site via a separate, third pipeline 91. Pumps raise the pressure of the contents of the third pipeline 91 to the extent necessary for them to traverse the length of the pipeline 91. However, it will be understood that the third pipeline 91 may be configured to accept some of the heat and some of the pressure energy released when the pressure and temperature of the final products pipeline are reduced via heat- and pressure-exchange equipment.Whether the third pipeline 91 is configured in this way, or simply used as a conduit for the return of this stream to the power station site, depends on the individual circumstances of the installation.\| [0101] 5 CHEMICAL REACTIONS\| [0102] The main chemical processes occurring throughout the process are as follows: 3CO2 + 3(NH4)2CO3 + 3H2O -» 6NH4HCO3 (4)\| [0103] 6NH4HCO3 -> 6NH3 + 6H2O + 6CO2 (5)\| [0104] 6CO2 + Mg3Si2O5(OH)4 -» 2SiO2Φ + 3MgCO3Ψ + 2H2O 0 + 6NH3 + 3CO2 (6)\| [0105] 3CO2 + 6NH3 + 3H2O -» 3(NILO2CO3 (7)\| [0106] NH3 + NH4HCO3 -» (NILO2CO3 (8)\| [0107] Equation 4 represents the absorption of carbon dioxide into the ammonia-rich5 ammonium carbonate aqueous phase to produce a solution comprising ammonium bicarbonate. On heating under pressures of at least 100 Bar in the reactor (i.e. pipeline or underground chamber), this ammonium bicarbonate decomposes to molecular ammonia, water and carbon dioxide according to equation 5. As shown in equation 6, under the high pressure and temperature conditions prevailing in the reactor the carbon O dioxide reacts with the serpentine (the chemical formula of which is shown in equation 6) or other silicate rock to form insoluble metal carbonates and silica, the final products of the process, which store the carbon dioxide. Equation 7 describes what happens after the reaction products are cooled to below 50°C, i.e. low enough to allow the free molecular ammonia and carbon dioxide to combine to form ammonium carbonate salts5 in solution. As shown, since much of the carbon dioxide has been absorbed by the metal silicate (here serpentine) the ratio of ammonia to carbon dioxide favour formation of the ammonia-rich normal carbonate. Additional normal ammonium carbonate may form according to equation 8, by reaction between ammonium bicarbonate, and free molecular ammonia. 0CONTROLLING ACIDITY IN THE SYSTEM\| [0108] As mentioned in preceding paragraphs, sulfate ions from SOx, and nitrate ions from NOx respectively, contained in the raw flue gases, may accumulate in the circulating solution of ammonium salts. Oxides of sulfur (SOx) are inevitable byproducts of the combustion of fossil fuels including coal, that incorporate sulfur- containing compounds in reduced form, for example pyrite (iron disulfide FeS2). Oxides of nitrogen (NOx) are also inevitable byproducts of the combustion of fossil fuels including coal, originating from nitrogen-containing compounds in the fuel, and from reactions between oxygen and nitrogen in air induced by the heat of the fuels' combustion, hi an Australian context, where coals tend to have low sulfur contents, and assuming use of modern "low-NOx burners", the rates of build-up of nitrate ions will not be high, but their build-up may still need to be limited to maintain the pH range to that most suited for the overall processes. When the SOx and NOx contained in flue gases contact the absorbent slurry as encountered in the scrubbing chamber 30 in the presence of additional oxygen including that contained in flue gases, a series of reactions occur that convert these gases to sulfates and nitrates: SOx to sulfate ions SO4— , and NOx to nitrate ions NO3-. In the normal course of separating out the insoluble solids for example magnesite and silica formed from the reactions between carbon dioxide and the metal silicates, as previously described, the soluble salts dissolved in the aqueous phase from the reactor including sulfates and nitrates are recycled for re-use in the scrubber, apart from the small quantities of such salts that are ultimately emplaced with the final product metal carbonates and silica. A consequence is that while carbon dioxide entering the system forms additional carbonate ions that are ultimately removed at an equal rate as insoluble metal carbonates, the tendency is for both sulfate and nitrate ions to accumulate in the circulating aqueous phase. In an embodiment, the system may implement a process for limiting the build-up of these ions (anions) to avoid an increase in the acidity (reduction in the pH number) of the circulating solution, as the formation of these ions leads to a concomitant formation of hydrogen ions in solution. It is noted that the system, to some extent, may inherently limit such a build-up by virtue of the fact that, as mentioned in the previous paragraph, not all soluble salts and other dissolved substances will be recovered by way of the solids-liquids separationprocess. To further reduce nitrate ion equilibrium concentration, it is necessary to limit correspondingly, the concentrations of NOx gases in the flue gases entering the scrubbing vessel 30. This may be achieved, for example, by using so-called 'low-NOx burners', and by other methods which achieve control of the combustion process to limit NOx formation in the power station's boilers.\| [0109] To control concentrations of sulfate ions in the circulating aqueous phase, the system 10 may employ an additional control mechanism 96 arranged to add/feed appropriate quantities of calcium oxide or hydroxide (which in water form calcium ions and hydroxyl ions) to a portion of the circulating slurry (a side-stream), wherein the sulfate ions react with it to form calcium sulfate, which mostly precipitates out as the sparingly soluble hydrated salt, gypsum:\| [0110] SO4" + Ca+* + 2H2O -» CaSO4.2H2O Ψ (9)\| [0111] Meanwhile, the hydroxyl ions combine with and neutralise a corresponding number of hydrogen ions (to form water molecules), thereby controlling (reducing) the acidity of the circulating solution.\| [0112] In an embodiment, calcium oxide generally may be naturally present in the power station fly ashes. If present in sufficient concentrations, the appropriate quantities of fly ash may be added by the control mechanism 96 to the circulating solution to control the pH levels to the desired ranges. If the quantities of calcium oxide naturally present in fly ash are inadequate, they may, in an embodiment, be augmented by adding pulverised limestone to raw power station flue gases in the boilers at one or more locations for example immediately upstream of the economiser section of the boilers, where flue gas temperatures are appropriate for the decomposition of limestone to calcium oxide and carbon dioxide (when exposed to furnace temperatures of 1,0000C or more, limestone is calcined to quicklime.\| [0113] Treatment processes applied to this side stream may also incorporate steps to recover base metals and other valuable components in solution, including nickel, copper and iron, hi one form, side-stream treatment may involve adding an inexpensive alkali, e.g. calcined lime, dolomite, limestone or the like. Sulfate ions can be removed via the following equation (shown for normal ammonium sulphate and calcium oxide):(NILt)2SO4 + CaO + 3H2O -» CaSO4.2H2θΨ + 2NH4OH (10) ammonium quicklime gypsum ammonium\| [0114] Sulfate hydroxide\| [0115] In an embodiment the control mechanism 96 may be further arranged to add fresh ammonia to the circulating solution, at an appropriate rate, to account for any losses of ammonia.\| [0116] FURTHER DETAIL OF ABSORPTION/SCRUBBING CHAMBER OPERATION Conditions in the absorption chamber 28 may be strongly oxidising to assist the conversion of the impurity gases dissolving in the aqueous phase of the slurry (i.e. SOx ending up as sulfates rather than sulfites, and NOx ending up as nitrates rather than nitrites). In an embodiment, the cool, saturated condition of the flue gases when in the absorption chamber 28, plus the partial pressure of oxygen in these gases of three per cent or more, may be sufficient to ensure oxidising conditions. As well, the large pool of slurry held in the bottom of the absorption chamber 28 may be aerated using compressed air as is normal practice with flue gas desulfurisation (FGD). However, if additional oxidising is required, the process may further involve irradiation of the flue gases immediately upstream of their entry into the absorption chamber 28 by electron beams or high- voltage brush discharge, to form free radicals from water and oxygen (OH" and 0~). These are powerful oxidising agents, able to convert rapidly, sulfur dioxide SO2 to the trioxide SO3, and nitric oxide NO to the dioxide NO2, the precursors to sulfates and nitrates respectively. Thus, the absorption chamber 28 may serve as a highly efficient scrubber for the removal of SOx and NOx. It may also remove volatile metals that may exist in trace quantities in coal and that end up in flue gases notably mercury (the low operating temperatures and oxidising environment will tend to favour the conversion of any mercury vapour present to non- volatile mercuric oxide, an insoluble solid that will accompany the final product metal carbonate and silica to their permanent emplacement).\| [0117] FURTHER DETAIL OF PRESSURE EXCHANGERS\| [0118] With reference to Fig. 4, there is shown an arrangement for the pressure- exchange apparatus described above. At the end of the reaction process, the pressure ofthe final carbonate-rich product must be reduced from approximately 120 Bar to atmospheric pressure. Instead of merely reducing pressure by throttling valves, thereby losing the energy embodied in this pressure, the energy this pressure represents may be conserved by transferring it to the extent possible, to the silicate slurry. In Fig. 4, slurry A comprises the products of the reactions that occur as the ammoniated, carbonated silicate slurry flow through the pipeline 44 from the power station to the mine site; while slurry B represents silicate slurry from the mine. A consequence of pressure exchange in these two stages is that slurry A's pressure would fall from around 120 Bar to near ambient pressure, while that of slurry B would rise from around atmospheric pressure to perhaps 100 Bar.\| [0119] Another pressure-exchange apparatus is also utilised at the power station site. Here, using the terminology of Fig. 4, slurry A represents the hot silicate slurry arriving via the pipeline from the mine; while slurry B comprises slurry exiting the scrubbing chamber 30 (i.e. silicate slurry now charged with ammonia and carbon dioxide, but at close to ambient pressures). A consequence of pressure exchange in this stage is that slurry A's pressure would fall from its arrival pressure (this may be 120 Bar, a pressure that would be maintained by booster pumping stations at strategic locations along the pipeline 44 to overcome friction losses), to near ambient pressure. This pressure may be transferred (exchanged) to the extent possible to slurry B, thereby minimising the amount of pumping energy required to raise the pressure of this slurry to the levels required, here assumed to be 120 Bar. Since slurry A at this point will be at well below 120 Bar, pressure-exchange between slurries A and B alone may not be capable of raising the pressure of slurry B to 120 Bar. Also, the volume of slurry B may exceed that of slurry A. This is because of the much higher contents of carbon dioxide and ammonia, and of water condensed out of the power station flue gases. In an embodiment, additional pumping capacity may be installed to boost slurry B pressures to those required for the pipeline 44, and to pressurise those (relatively small) quantities of slurry B that cannot be pressurised by pressure-exchange with slurry A. For this function, conventional high-pressure diaphragm pumps, such as the Geho pump manufactured by Weir Netherlands b.v., may be implemented. This pumping, together with the pumping energy required to maintain pressures along the length of the pipelines, account for a substantial proportion of the total mechanical energy input to the total process. Other suitable pressure exchange/pump-turbine sets may comprisecentrifugal pumps and radial-type hydraulic turbines. As the pressures are relatively high, the type of centrifugal pump may be a multi-stage barrel-type pump.\| [0120] With reference to Fig. 5 there is shown a configuration for the heat exchanger arrangements 40 & 46, according to an embodiment of the present invention. As previously discussed, high temperatures are required to initiate and accelerate the carbon sequestration reactions: the conversion of metal silicates to carbonates. These reactions, being exothermic, yield additional heat that can and should be applied to assist with creating the conditions needed for these reactions to proceed most efficiently. As shown, the heat-exchanger arrangement is in the form of a simple shell- and-tube heat exchanger, consisting of two concentric pipes: the inner forms the "tube", the outer, the "shell". An advantage with this arrangement is that the heat exchanger can be made as long as is required to affect the desired transfer of heat: if necessary, many hundreds of metres long. For heat exchanger 40 (i.e. the heat exchanger on the silicate rock quarry site side), heat energy is transferred between the final carbonate/silica product (i.e. slurry A), which is hot, and the silicate slurry (slurry B), which is cool. For heat exchanger 46 (i.e. the heat exchanger on the power station side), slurry A would be hot silicate slurry from the quarry, while slurry B would be slurry exiting the scrubbing chamber 30 (i.e. now charged with ammonia and carbon dioxide, but at close to ambient temperatures).\| [0121] UNDERGROUND REACTOR\| [0122] Turning now to Fig. 2, there is shown an alternative system 200 for performing carbon dioxide sequestration which utilises (where geological conditions permit) an underground chamber as the reactor, as opposed to a pipeline reactor as illustrated in Fig. 1. In this embodiment, the reactor is in the form of a chamber 70 excavated from bedrock at a depth sufficient to allow the conditions for the core carbonation reactions to be generated entirely or partly by static head alone (e.g. 100 Bar). A chamber 70 excavated at a depth of approximately 800 meters and having a volume of 300,000 cubic meters, sufficient to allow for a 24 hours' detention time for the contents, may be envisaged for holding the reactive slurry output from a system 200 fitted to an efficient\| [0123] 1,000MWe coal-fired power station. In practice a smaller chamber may suffice, should it arise that the reactions are essentially completed in less time.\| [0124] The silicate slurry 36 may be prepared either at the serpentine quarry site andpumped overland to the power station site, or, the mineral could be railed, trucked or otherwise suitably transported to the power station site, and prepared there. Were the former implementation adopted, pipeline arrangements 44 would be considerably simpler than for the pipeline reactor embodiment described above with reference to Fig. 1. Specifically, the silicate slurry 36 would not be required to collect and transport heat and pressure energy from the quarry site to the power station site, nor to host any residual ammonium salts. The pipeline 44 would simply be utilised for mineral transport; whether it was transported as a lump product by rail or as slurry by pipeline would be determined by economic and environmental considerations. It will be appreciated that in this embodiment, silicate slurry density may be substantially higher (e.g. 60 per cent solids by weight), thereby reducing the volumes of silicate slurry required to be pumped, and allowing a lower pipeline velocity because of the reduced tendency for the solids in denser slurries to segregate and silt up the pipeline 44. Also, arrangements for conserving heat and pressure are much simpler than they would need to be for the pipeline reactor alternative.\| [0125] In Fig. 2, an injection pump 72 is utilised to drive the circulation of the reactive slurry from the scrubbing chamber 40, through a plurality of counter-current heat exchangers 74, 76, underground reactor 70 and counter-current decantation system for the separation of normal ammonium carbonate and other salts in the aqueous phase of the products of the underground reactor, and the insoluble carbonated mineral solids that are to be emplaced permanently.\| [0126] Heat exchangers 74, 76 are shown in schematic form at two locations on Fig. 2. The heat exchangers 74, 76 may be long, shell-and-tube designs, as shown in Fig. 4: they may span most of the vertical distance from the scrubbing chamber 40 down to the underground chamber 70. This is to say, whereas two separate pipelines are implied in Fig. 2, in practice, for most of their length they may be concentric: the annulus formed between the outer and concentric inner pipe transporting the hot reaction products, while the inner pipe transports the products heading downward to the Reaction chamber. It will be understood by persons skilled in the art that this selection may be reversed.\| [0127] In contrast to the pipeline reactor configuration shown in Fig. 2, heating of the reactive slurry may be accomplished by exchanging heat from the hot reaction productsrising first from the ammonia gas recovery vessel 78, and as the raw slurry descends further, from hot slurry rising from the underground chamber 70. While some supplementary heat may be required, the heat generated by Equation 2(b) would be conserved, and available to heat raw reactive slurry. The design of the underground chamber 70 may be optimised to achieve some plug- flow characteristics. In an embodiment, the chamber 70 may have a high length- to-diameter ratio of 10: 1 and be vertically aligned. Utilising a vertically aligned chamber provides that the incoming reactive slurry, being cooler hence slightly denser than the average contents of the reactive chamber 70, will tend to stratify at lower levels, displacing hotter slurry upwards. In an embodiment, the underground chamber 70 may be subdivided into two or more vertically stacked sub-chambers.\| [0128] In an embodiment, the reactive chamber 70 may employ an agitator (not shown) to maintain the solids in suspension. This may be advantageous where large residence times are required, implying in turn large reactor volumes. As will readily be appreciated, heat losses from the underground chamber 70 and pipelines may be much smaller than they would be even from a lagged above- ground pipeline and may be further reduced by insulation surrounding the reactor, pipelines and any other underground process vessels. Whereas an overland pipeline represents a plug-flow reactor, ideal conditions for a relatively slow series of reactions as are involved in carbon sequestration are also obtained in the embodiment illustrated in Fig. 2.\| [0129] It is noted that in the Fig 2 embodiment, the two overflow streams from the CCD system are handled separately. The overflow of the first thickener tank 90a is blended with the silicate slurry 36, incoming from the quarry site to form the circulating solution to be sent to the absorption chamber 28.\| [0130] The balance of the process in relation to sequestration, separation and emplacement is as for the overland pipeline reactor case.Example\| [0131] Again with specific reference to Fig. 3, a non-limiting example process flow for carbon sequestration for the first system configuration 10 described herein (i.e. the system depicted in Fig. 1) will now be given, wherein for convenience, like parts to those shown in the foregoing embodiment have been numbered with like numerals.\| [0132] Example 1\| [0133] Table 1: Indicative mass balance figures from 1.000 MWe of black coal-fired electricity generation plant. Material Per year Per hour\| [0134] Total CO2 generated: 6.4 m. tonnes 80O t\| [0135] (NKU)2CO3 to absorb 90% of this CO2 1,60O t\| [0136] Resulting quantity OfNH4HCO3 formed 2,400 1\| [0137] Water to make up 25% solution OfNH4HCO3 7,200 t Serpentine to absorb 90% of this CO2, 80% eff. 17.2 m tonnes 2,150 t\| [0138] Total slurry with NH4HCO3: 9,350 t\| [0139] Slurry density: 1.2 t/m3 1.2 t/m3\| [0140] Slurry volume, m3 8,000 m3\| [0141] Product (carbonate plus silica) solids: 20.6 m. tonnes 2,600 1 Slurry pipe dia. with 3 m/s velocity: 1.0 metres 1.0 metres\| [0142] Ammonia lost due to SOx (90% recovery via Eq. 10) ) 11,,66000O 1t 0.2 t\| [0143] Ammonia lost due to NOx 3,0001 0.37 t\| [0144] Total losses of ammonia: 4.600 1 0.57 t\| [0145] Table 1 provides an indicative detailed mass balance for a carbon dioxide sequestration process, assuming:\| [0146] - 90 per cent carbon dioxide capture and sequestration from 1,000 MWe of black coal- fired electricity generation plant, which when operating in base-load mode might expect to generate annually 8,000 GWh of electricity; - where on a dry ash-free basis, the coal is 81.3% by weight carbon and 0.65% sulphur (as S) and the flue gases contain 400 ppm NOx.An advantage of the carbon dioxide sequestration process 100 and systems 10, 20 according to embodiments of the present invention is that by selecting ammonia as a catalyst/promoter, a single integrated process can be provided for both capture and sequestration of carbon dioxide. In an embodiment, sequestration of the carbon dioxide takes place in a reactor, in the form of a return pathway 52 of a pipeline 44, which advantageously connects the power station (i.e. the source of carbon dioxide) to the source/destination of the absorbent material being used in the process, hi an alternative embodiment, where geological conditions permit, the reactor may take the form of an underground chamber which advantageously facilitates the reaction without requiring pressure-exchange and head-recovery equipment required for the pipeline embodiment. Another advantage of the carbon dioxide sequestration process and systems is that the reaction kinetics may be improved by using ammonia. Therefore, by using ammonia and exploiting the heat generated by the exothermic reaction, the energy consumption of the process 100 can be kept to a minimum. As the reaction products are thermodynamically stable, carbon dioxide can be stored in a permanent stable solid form. Following from this, further advantages include lower operating and capital costs.\| [0147] Persons skilled in the art will appreciate that further advantages may arise from carrying out certain steps of the aforementioned embodiments in isolation. For example, the catalytic effect of a solution of ammonia with an ammonium salt (that may be ammonium carbonate formed by exposing an ammonia-rich solution to a gas stream containing carbon dioxide) in the carbon dioxide sequestration process can also be utilised for extracting metals (e.g. magnesium, iron, nickel, copper and other metals present in the silicate rock) from metal silicates, such as magnesium-rich metal silicates. In such an embodiment a solution of ammonia-rich ammonium carbonates in water may be mixed with a metal silicate (typically in slurry form) to allow the dissolution of magnesium ions by ammonia to recover the metal, in this embodiment a metal compound in the form of magnesium carbonate. The mixing may occur in an ammonia absorption chamber such as that previously described in connection with the preceding embodiments. Preferably the solution contains molecular ammonia in the presence of ammonium salts in solution, such as ammonium carbonate, to prevent the precipitation of magnesium hydroxide, hence allowing the dissolution of magnesium ions by ammonia to continue, substantially free of concerns over tendencies for otherwiseinsoluble magnesium hydroxide to coat, and restrict access to the silicate mineral by carbon dioxide and ammonia. A further advantage arising from this process is that after extraction of magnesium carbonate, other minerals (metals) present within the silicate rock are also amenable to recovery. The silicate rock may comprise mafic or ultra- mafic rocks (i.e. rocks with respectively a high or very high ratio of magnesium to silicon content).\| [0148] Expressed another way, the catalytic effect of the ammonia follows from its tendency to form complexes (ammines) with certain metal ions including magnesium (Mg2+), divalent iron (Fe2+), copper (Cu2+) and nickel (Ni2+). The presence of ammonium salts notably the various carbonates formed from the reaction between ammonia and carbon dioxide prevents precipitation of the otherwise insoluble magnesium hydroxide. Magnesium carbonate is however insoluble in such an environment, so a precipitate of this compound will form from the reaction between magnesium hydroxide and ammonium carbonate, to yield ammonium hydroxide and free molecular ammonia in solution, the latter continuing to extract additional magnesium and other metals from the silicate rock through formation of ammine complexes until all such susceptible metals have been extracted.\| [0149] Finally, it is to be appreciated that various alterations or additions may be made to the parts previously described without departing from the spirit or ambit of the present invention. The process is not limited to having a single two-stage continuous reactor, or a single tube-like reactor, as the process may be arranged to utilise alternatively configured items of equipment as necessary to accommodate process variables, arising from different source materials, capital and operating costs. For example, in the exemplary embodiment previously described the plant design is based on the emission of 800 tonnes CO2/GWh generated from a state-of-the-art black coal- fired electricity generation plant. By comparison, the Bayswater Power Station and the Liddell Power Station, both in the Hunter Valley of New South Wales, Australia, able to generate 2,640 MWe and 2,040 MWe respectively, being older hence less efficient can be expected to emit between 850 and 900 tonnes CO2/GWh. Thus the concentration and rate of carbon dioxide emissions in the flue gas emitted by the power plant may vary such that the plant equipment design may be reconfigured to accommodate these variables. For example, alternative equipment can be configured for the various heat and pressure exchange stations. The carbon dioxideabsorption zone and the scrubbing zone may be arranged in series in two separate vessels (rather than the nested configuration shown in Fig. 1). The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s). As well, the corresponding solids concentration in the slurry feed may be higher or lower than 25% solids by weight. It is possible that the metal silicate solution may comprise a blend of metal silicates, e.g. mixture of serpentines and olivines, even pyroxenes. The reaction kinetics may require heat to be removed from the reactive solution (rather than heat addition as described above). These factors will impact and alter the system pressures. There might be two or more pipelines for transporting the metal silicate solution and the reactive solution; because there are more pipelines, additional heat exchangers and pressure-exchange apparatus may be used. The power station flue gas may include additional pre-processing steps including flue gas desulphurisation (FGD) and selective catalytic reduction (SCR) to reduce concentrations of SOx and NOx respectively hence losses of ammonia from the system. Furthermore, the availability of services, such as steam and cooling water may require different equipment arrangements.\| [0150] Any reference to prior art contained herein is not to be taken as an admission that the information is common general knowledge, unless otherwise indicated.\| [0151] In the claims which follow and in the preceding description of the invention, except where the context requires otherwise due to express language or necessary implication, the word "comprise" or variations such as "comprises" or "comprising" is used in an inclusive sense, i.e. to specify the presence of the stated features but not to preclude the presence or addition of further features in various embodiments of the invention.	Family Number\|(1878278)\|1878278\|Object of Invention\|(AU2010210311 A1)\| (...) absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock\|3 0 In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of: (i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium (...) ammonium carbonate to produce a solution comprising ammonium bicarbonate; (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\|(CN102395417 A)\|In a first aspect , the present invention provides a method for sequestration of carbon dioxide comprising the steps of : \|The present invention provides a carbon dioxide capture and sequestration process comprising a first stage of scrubbing a carbon dioxide containing gas stream with a solution containing normal ammonium carbonate capable of absorbing carbon dioxide , wherein the carbon dioxide reacts with the ammonium ( . . . ) \|The present invention relates generally to systems , devices and methods for carbon dioxide sequestration , and more particularly , but not exclusively , to systems and methods for capturing and sequestering carbon dioxide from flue gases of coal - fired power plants . \|(WO201088738 A1)\|Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\|hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and (...) In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|(IN2011DN06815 A)\|Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\|hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and (...) In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|Abstract\|(AU2010210311 A1)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|(CN102395417 A)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate . In a second stage , a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica . \|(EP2393577 A4)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|(WO201088738 A1)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|(IN2011DN06815 A)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate.In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|Title\|(AU2010210311 A1)\|System, apparatus and method for carbon dioxide sequestration\|(CN102395417 A)\|System , apparatus and method for carbon dioxide sequestration \|(EP2393577 A4)\|System, apparatus and method for carbon dioxide sequestration\|(EP2393577 A1)\|System, apparatus and method for carbon dioxide sequestration\|(WO201088738 A1)\|System, apparatus and method for carbon dioxide sequestration\|(IN2011DN06815 A)\|System, apparatus and method for carbon dioxide sequestration\|(HK1164777 A)\|System, apparatus and method for carbon dioxide sequestration\|Advantages / Prev. Drawbacks\|(WO201088738 A1)\|The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage).\|(IN2011DN06815 A)\|The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage).\|Independent Claims\|(AU2010210311 A1)\|1. A carbon dioxide sequestration process including the steps of: (...) (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| (...) absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|36. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|(CN102395417 A)\|1. A method of carbon dioxide sequestration comprising the steps of : ( . . . ) ( ii ) passing a reaction slurry comprising metal silicate rock and an ammonium bicarbonate solution through a reactor , the reactor being controlled so as to promote a reaction between the ammonium bicarbonate and the silicate rock to produce metal carbonate and silica . \|( . . . ) ( b ) a reactor for receiving a reaction slurry comprising metal silicate rock and ammonium bicarbonate produced by ( a ) , the reactor being controlled so as to promote a reaction between the ammonium bicarbonate and the metal silicate to produce a metal carbonate and silica . \|38. Providing a first fluid channel in the pipeline , the first fluid channel transporting a metal silicate slurry for use by a first apparatus in a carbon sequestration process ; and a second fluid passageway that carries the reacted ammonium bicarbonate - metal silicate slurry from the first apparatus , wherein the second fluid passageway is controlled so as to promote reaction of the bicarbonate with the metal ( . . . ) \|39. A process for reacting a slurry comprising metal silicate rock and an aqueous phase comprising an ammonium bicarbonate solution to produce a metal carbonate , the process comprising the steps of : \|(WO201088738 A1)\|1. A carbon dioxide sequestration process including the steps of: (...) (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| (...) (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|38. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and (...) \|39. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|(IN2011DN06815 A)\|1. A carbon dioxide sequestration process including the steps of: (i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium (...) ammonium carbonate to produce a solution comprising ammonium bicarbonate; (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| (...) absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|38. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and (...) \|39. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|	Chemical engineering\|Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-053/77\|B01D-053/96\|B01D-2251/206\|B01D-2251/606\|B01D-2257/504\|C01B-032/60\|Y02C-020/40\|Y02P-020/151		B01D-053/62\|B01D-053/77\|B01D-053/96\|B01D-2251/206\|B01D-2251/606\|B01D-2257/504\|C01B-032/60\|Y02C-020/40\|Y02P-020/151	B01D\|B01D-053/62\|B01D-053/96\|C01B\|C01B-032/50\|C01B-032/60	B01D\|B01D-053/62\|B01D-053/96\|C01B\|C01B-031/20\|C01B-031/24			WO2024208737\|EP4442351\|WO202444690\|EP4353956;EP4353956\|EP4051414;EP4051414\|CN111715146\|CN108710778\|CN108031242\|CN107021488\|WO201599612\|CN103974757\|EP2763783;EP2763783\|WO201349896\|DE102024201178\|EP4359113\|DE102021116491\|US12409413\|CN108139502B\|US9896741\|WO201228418\|CN102114383B\|CN102078743B	WO2024208737 111711345 WHO=Examiner SELF=N CAT=X CAT=I\|EP4442351 111711345 WHO=Examiner SELF=N CAT=X CAT=I\|WO202444690 108683267 WHO=Examiner SELF=N CAT=A\|EP4353956 98745634 WHO=Examiner SELF=N CAT=A\|EP4051414 93920984 WHO=Examiner SELF=N CAT=A\|CN111715146 90806865 WHO=Examiner SELF=N CAT=A\|CN108710778 81767099 WHO=Examiner SELF=N CAT=A\|CN108031242 79710421 WHO=Examiner SELF=N CAT=A\|CN107021488 75106585 WHO=Examiner SELF=N CAT=A\|WO201599612 69805816 WHO=Examiner SELF=N CAT=A\|CN103974757 44920168 WHO=Examiner SELF=N CAT=A\|EP2763783 44920168 WHO=Examiner SELF=N CAT=A\|WO201349896 44920168 WHO=Examiner SELF=N CAT=A\|DE102024201178 115623811 WHO=Examiner SELF=N\|EP4359113 103205323 WHO=Examiner SELF=N\|DE102021116491 103205323 WHO=Unknown SELF=N\|US12409413 93920984 WHO=Applicant SELF=N\|CN108139502B 76398916 WHO=Examiner SELF=N\|US9896741 69805816 WHO=Applicant SELF=N\|WO201228418 18771696 WHO=Applicant SELF=N\|CN102114383B 7351345 WHO=Examiner SELF=N\|CN102078743B 7290484 WHO=Examiner SELF=N	AU2008217572\|AU2008217572\|WO2008101293\|WO200760149\|WO200760149\|US20080031801\|US20080031801\|CN101010129\|CN1153482	AU2008217572 6597398 WHO=Examiner SELF=N CAT=X\|AU2008217572 6597398 WHO=Examiner SELF=N CAT=X\|WO2008101293 6597398 WHO=Examiner SELF=N CAT=X\|WO200760149 5345427 WHO=Examiner SELF=N CAT=A\|WO200760149 5345427 WHO=Examiner SELF=N CAT=A\|US20080031801 43690578 WHO=Examiner SELF=N CAT=A\|US20080031801 43690578 WHO=Examiner SELF=N CAT=A\|CN101010129 76566186 WHO=Examiner SELF=N CAT=A\|CN1153482 1355390 WHO=Examiner SELF=N CAT=A		AU2008217572; US20080031801; WO200760149\|\|\|AU2008217572; US20080031801; WO200760149\|CN1153482; CN101010129; WO2008101293\|	(EP2393577)\|Search Report references [Examiner]\|-No further relevant documents disclosed\|-See also references of WO 2010088738A1\|\|(WO2010/088738)\|International Search Report [Examiner]\|-See also references of EP 2393577A4\|\|\|\|\|	LAPSED	(EP2393577)\|LAPSED\|(WO2010/088738)\|LAPSED\|(CN102395417)\|LAPSED\|(IN6815/DELNP/2011)\|LAPSED\|(HK1164777)\|LAPSED\|(AU2010210311)\|LAPSED	DEAD	(EP2393577)\|DEAD\|(WO2010/088738)\|DEAD\|(CN102395417)\|DEAD\|(IN6815/DELNP/2011)\|DEAD\|(HK1164777)\|DEAD\|(AU2010210311)\|DEAD	(EP2393577)\|LEGAL DETAILS FOR EP2393577\|Actual or expected expiration date=2014-09-02\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-08\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP10738163\|Application date=2010-02-08\|Standardized application number=2010EP-0738163\|Event publication date=2011-11-11\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2011-12-14\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2393577\|Publication stage code=A1\|Publication date=2011-12-14\|Standardized publication number=EP2393577\|Event publication date=2011-12-14\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2011-09-06\|Event publication date=2011-12-14\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR\|Event publication date=2012-05-16\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2012-08-01\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP2393577\|Publication stage code=A4\|Publication date=2012-08-01\|Standardized publication number=EP2393577\|Event publication date=2012-08-01\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2012-06-29\|Event publication date=2012-08-01\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-08-01\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-08-01\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2015-01-16\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2015-02-18\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2014-09-02\|MEMBER STATE LEGAL DETAILS FOR HK\|Actual or expected expiration date=2018-08-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HK Corresponding appl: HK1164777\|Event publication date=2012-09-28\|Event code=EP/REG\|Event code=HK/DE\|Event group=Examination events\|Reference to a national code\|Requests to designate patent in hong kong\|Requests to record published in hong kong\|Corresponding cc:\|Designated or member state=HK\|Event publication date=2018-08-31\|Event code=EP/REG\|Event code=HK/WD\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Applications withdrawn, deemed to be withdrawn, or refused after publication in hong kong\|Corresponding cc:\|Designated or member state=HK\|(WO2010/088738)\|LEGAL DETAILS FOR WO2010/088738\|Actual or expected expiration date=2012-08-06\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-08\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOAU2010000124\|Application date=2010-02-08\|Standardized application number=2010WO-AU00124\|Event publication date=2010-08-12\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2010088738\|Publication stage code=A1\|Publication date=2010-08-12\|Standardized publication number=WO201088738\|Event publication date=2012-08-06\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2010210311\|Actual or expected expiration date=2014-09-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2010210311\|Application date in the designated or member state=2010-02-08\|Application number in the designated or member state=2010AU-0210311\|Corresponding cc:\|Designated or member state=AU Corresponding pat: 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national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP2393577\|Actual or expected expiration date=2014-09-02\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP10738163\|Application date in the designated or member state=2010-02-08\|Application number in the designated or member state=2010EP-0738163\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2393577\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2011-12-14\|Publication number in the designated or member state=EP2393577\|Event publication date=2010-09-29\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2011-09-06\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national 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state=HK\|MEMBER STATE LEGAL DETAILS FOR IN6815/DELNP/2011\|Actual or expected expiration date=2022-12-14\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN6815/DELNP/2011\|Application date in the designated or member state=2011-09-06\|Application number in the designated or member state=2011IN-DN06815\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN6815/DELNP/2011\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-12-14\|Publication number in the designated or member state=IN2011DN06815\|Event publication date=2011-09-06\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|Event publication date=2012-12-14\|Event code=IN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IN\|(CN102395417)\|LEGAL DETAILS FOR CN102395417\|Actual or expected expiration date=2014-12-03\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-08\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201080013080\|Application date=2010-02-08\|Standardized application number=2010CN-80013080\|Event publication date=2012-03-28\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN102395417\|Publication stage code=A\|Publication date=2012-03-28\|Standardized publication number=CN102395417\|Event publication date=2012-03-28\|Event code=CN/C06\|Event indicator=Pos\|Event group=Examination events\|Publication\|Event publication date=2012-05-09\|Event code=CN/C10\|Event group=Examination events\|Request of examination as to substance\|Event publication date=2014-12-03\|Event code=CN/C02\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Deemed withdrawal of patent application after publication (patent law 2001)\|(IN6815/DELNP/2011)\|LEGAL DETAILS FOR IN6815/DELNP/2011\|Actual or expected expiration date=2022-12-14\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-09-06\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN6815/DELNP/2011\|Application date=2011-09-06\|Standardized application number=2011IN-DN06815\|Event publication date=2012-12-14\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN6815/DELNP/2011\|Publication stage code=A\|Publication date=2012-12-14\|Standardized publication number=IN2011DN06815\|Event publication date=2022-12-14\|Event code=IN/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(HK1164777)\|LEGAL DETAILS FOR HK1164777\|Actual or expected expiration date=2017-09-28\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-14\|Event code=HK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=HK HK12105806\|Application date=2012-06-14\|Standardized application number=2012HK-0105806\|Event publication date=2012-09-28\|Event code=HK/A\|Event indicator=Pos\|Event group=Examination events\|Standard patent (R) application\|Publication country=HK\|Publication number=HK1164777\|Publication stage code=A\|Publication date=2012-09-28\|Standardized publication number=HK1164777\|Event publication date=2017-09-28\|Event code=HK/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(AU2010210311)\|LEGAL DETAILS FOR AU2010210311\|Actual or expected expiration date=2014-09-04\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-08\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2010210311\|Application date=2010-02-08\|Standardized application number=2010AU-0210311\|Event publication date=2011-09-01\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2010210311\|Publication stage code=A1\|Publication date=2011-09-01\|Standardized publication number=AU2010210311\|Event publication date=2014-09-04\|Event code=AU/MK4\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application lapsed section 142(2)(d) - no continuation fee paid for the application	(EP2393577)\|Contracting States: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2010/088738)\|ARIPO: GH, GM, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2010/088738)\|EAPO: RU, TJ, BY, MD, AZ, TM, AM, KG, KZ\|(WO2010/088738)\|EPO: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2010/088738)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2010/088738)\|National States: PT, HN, HR, HU, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KM, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PE, PG, PH, PL		https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=NoFk66ibPDQqLsHudby62XmXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO201088738&ekey=1500&xpn=EP2393577&kind=A4	https://register.epo.org/application?number=EP10738163	https://permalink.orbit.com/RenderStaticFirstPage?XPN=DDKAB7Lhfd7dGqGyRhNS9XfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	AU	(WO2010/088738)\|AU	(WO2010/088738)\|NAME=HUNWICK, Richard, J. 59 Abingdon Road, Roseville, New South Wales 2069 , COUNTRY=AU	(EP2393577)\|BE\|(EP2393577)\|BE\|(WO2010/088738)\|AU\|\|(HK1164777)\|HK\|(AU2010210311)\|AU	(EP2393577)\|NAME=De Clercq, Ann G. Y.;De Clercq & Partners Edgard Gevaertdreef 10a , CITY=9830 Sint-Martens-Latem , COUNTRY=BE , REG=101201288\|(EP2393577)\|NAME=De Clercq, Ann G. Y.;De Clercq & Partners Edgard Gevaertdreef 10a , CITY=9830 Sint-Martens-Latem , COUNTRY=BE , REG=101201288\|(WO2010/088738)\|NAME=GRIFFITH HACK Level 29, Northpoint, 100 Miller Street, North Sydney, New South Wales 2060 , COUNTRY=AU\|(CN102395417)\|NAME=LIU JIFU;CHINABLE INTELLECTUAL PROPERTY NAME=WANG LEI;CHINABLE INTELLECTUAL PROPERTY\|(HK1164777)\|NAME=MARKS & CLERK , COUNTRY=HK\|(AU2010210311)\|NAME=Griffith Hack Level 29, Northpoint 100 Miller Street , CITY=North Sydney , STATE=NSW , POSTCODE=2060 , COUNTRY=AU	(EP2393577)\|AU\|(EP2393577)\|AU\|(WO2010/088738)\|AU\|\|(IN6815/DELNP/2011)\|AU\|\|	(EP2393577)\|NAME=Hunwick, Richard J. 59 Abingdon Road, CITY=Roseville NSW 2069, COUNTRY=AU\|(EP2393577)\|NAME=Hunwick, Richard J. 59 Abingdon Road, CITY=Roseville NSW 2069, COUNTRY=AU\|(WO2010/088738)\|NAME=HUNWICK, Richard, J. 59 Abingdon Road, Roseville, New South Wales 2069, COUNTRY=AU\|(CN102395417)\|NAME=HUNWICK RICHARD J\|(IN6815/DELNP/2011)\|NAME=HUNWICK RICHARD J, COUNTRY=AU\|(HK1164777)\|NAME=Hunwick Richard J\|(AU2010210311)\|NAME=Hunwick, Richard J.	(WO2010/088738)\|6\|(IN6815/DELNP/2011)\|6\|(CN102395417)\|6\|(AU2010210311)\|6	3	6			(EP2393577)\|WO2010/088738\|(CN102395417)\|WO2010/088738\|(IN6815/DELNP/2011)\|WO2010/088738\|(HK1164777)\|WO2010/088738\|(AU2010210311)\|WO2010/088738		Primary examiner: Polesak, Helmut\|\|Primary examiner: Polesak, Helmut\|\|(WO2010/088738)\|Number of Claims: NCL=45\|Extended kind: EXTK=x\|\|(CN102395417)\|Number of Claims: NCL=45\|Gazette date: GAZDATE=2012-03-28\|Gazette number: GAZNUM=28-13\|Substantial examination effective date: 20120509\|Number of Pages: NPAGES=26\|\|(IN6815/DELNP/2011)\|Number of Claims: NCL=45\|\|(AU2010210311)\|Number of Claims: NCL=13\|		(EP2393577)\|ENGLISH (ENG)	(IN2011DN06815)\|Patent\|(HK1164777)\|Patent\|(EP2393577)\|Patent\|(CN102395417)\|Patent\|(EP2393577)\|Patent\|(AU2010210311)\|Patent\|(WO201088738)\|Patent	Titre: (EP2393577)\|System, apparatus and method for carbon dioxide sequestration Résumé: (EP2393577)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.	2	Abstract	gpt-4o-mini	yes	The patent describes a process that involves the reaction of ammonium bicarbonate with metal silicate rocks to produce metal carbonates, which aligns with the topic of enhanced weathering and CO₂ sequestration.
6	CN202411977823	CN202411977823	CN119607861	113778323	CN119607861 A 2025-03-14 [CN119607861]	2024-12-31	2024-12-31	2025-03-14		(CN119607861)\|2044-12-31	(CN119607861)\|Carbon capture and storage system and carbon capture and storage method	(CN119607861)\|The invention relates to the technical field of flue gas treatment, in particular to a carbon capture and storage system and a carbon capture and storage method.The carbon capture and storage system comprises a waste gas absorption unit, an amine liquid circulation unit, a carbon dioxide gas salinization unit and a carbon sequestration unit which are communicated in sequence; the system further comprises a limestone slurry pulping and filling unit; and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. The carbon capture and storage method is a brand-new organic amine decarburization and permanent carbon sequestration method provided on the basis of the principle of enhancing rock weathering; compared with a traditional carbon sequestration method that carbon dioxide is transported through compression and liquefaction and stored in an underground salt water layer, the method has the advantages that the carbon capturing and storing process is short, high-pressure and low-temperature high-energy-consumption equipment does not need to be used, the captured carbon dioxide gas does not need to be stored and transported at low temperature, energy consumption can be reduced, the carbon sequestration cost is saved, and the carbon sequestration efficiency is improved. The carbon dioxide escape phenomenon in the storage and transportation process can be avoided, and the carbon sequestration efficiency is improved.	SINOTECH ENERGY\|ZHONGTAI CARBON SHANGHAI ENVIRONMENTAL PROTECTION SCIENCE & TECHNOLOGY	(CN119607861)\|SINOTECH ENERGY CO., LTD. ([CN])\|ZHONGTAI CARBON SHANGHAI ENVIRONMENTAL PROTECTION SCIENCE AND TECH LIMITED COMPANY	WEI YING\|HE WEI	(CN119607861)\|WEI YING\|HE WEI		(CN119607861)\|Compared with the prior art, the invention has the advantages that: (1) The invention provides a carbon capture storage system and a carbon capture storage method, wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine, then resolving the carbon dioxide gas in a desorption tower, then reacting the resolved carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, and finally sealing the calcium bicarbonate in a deep sea discharge area; compared with the traditional carbon fixation method of carbon dioxide through compression, liquefaction and transportation and underground salty water layer sealing, the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short, high-pressure and low-temperature high-energy equipment is not needed in the carbon capture and sealing process, the low-temperature storage and transportation of captured carbon dioxide gas are not needed, the energy consumption can be reduced, the carbon fixation cost can be saved, the phenomenon of carbon dioxide escape in the storage and transportation process can be avoided, the carbon fixation efficiency is improved, meanwhile, the consumption in the aspects of manpower and material resources can be reduced, and the problems of overlong carbon capture and sealing flow, high energy consumption, high cost, high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved.\|	(CN119607861)\|1. The carbon capturing and storing system is characterized by comprising an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit, a carbon fixation and sealing unit and a limestone slurry pulping and filling unit; The waste gas absorption unit comprises a temperature reduction tower and an absorption tower, wherein the upper part of the temperature reduction tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reduction tower is communicated with the absorption tower, a seawater spraying device is arranged in the temperature reduction tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reduction tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through a water conveying pipeline, the bottom of the temperature reduction tower is also provided with a seawater outlet, the upper end in the absorption tower is provided with a lean amine liquid spraying device, and the top of the absorption tower is provided with an exhaust port; The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. \|	(CN119607861)\|The invention provides a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.Disclosure of InventionThe invention aims to provide a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|The invention relates to the technical field of flue gas treatment, in particular to a carbon capture storage system and a carbon capture storage method.\|The invention relates to the technical field of flue gas treatment, in particular to a carbon capturing and storing system and a carbon capturing and storing method, comprising an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salifying unit and a carbon fixing and sealing unit which are sequentially communicated; the device also comprises a limestone slurry pulping and filling unit which is communicated with the carbon dioxide gas salinization unit.\|	(CN119607861)\|DESORPTION TOWER(100,39)\|CARBON CAPTURE(100,17)\|CARBON(100,15)\|CARBON CAPTURE STORAGE(100,13)\|STORAGE SYSTEM(100,13)\|CARBON CAPTURE STORAGE SYSTEM(100,11)\|LIMESTONE SLURRY POND(87,21)\|CARBONIZATION TANK(85,38)\|ABSORPTION TOWER(84,60)\|LIMESTONE SLURRY(74,32)\|SLAG DISCHARGE(72,6)\|AMINE DECARBURIZATION STORAGE(62,4)\|REGENERATING GAS COOLER(57,14)\|ORGANIC AMINE DECARBURIZATION STORAGE(54,4)\|CONVEYING PIPELINE(51,9)\|DECARBURIZATION STORAGE(51,4)\|SLURRY POND(49,21)\|SEAWATER PUMP(49,9)\|GAS SALINIZATION(48,8)\|FLUE GAS CONVEYING PIPELINE(44,9)\|ORGANIC AMINE DECARBURIZATION(44,1)\|LEAN AMINE LIQUID(42,27)\|AMINE DECARBURIZATION(42,1)\|CARBONIZATION TANK BOTTOM(38,12)\|AMINE LIQUID(37,54)\|COMPRESSOR(35,26)\|CARBON DIOXIDE GAS SALINIZATION(35,8)\|CONVEYING LIMESTONE SLURRY RESIDUE(34,2)\|BUBBLE DISTRIBUTOR(33,8)\|LEAN LIQUID COOLER(32,6)\|SEAWATER(31,27)\|COOLED LEAN AMINE(31,4)\|LEAN RICH LIQUID INLET(30,2)\|GAS SALIFYING(29,2)\|MANPOWER(29,2)\|WATER CONVEYING PIPELINE(29,2)\|ENHANCED ROCK(29,1)\|RICH AMINE LIQUID(28,19)\|CONVEYING LIMESTONE POWDER(28,2)\|OVERLONG CARBON CAPTURE(28,1)\|CARBON DIOXIDE(27,65)\|TEMPERATURE REDUCTION TOWER(27,29)\|AMINE LIQUID CIRCULATION(27,6)\|LIMESTONE SLURRY TANK(27,4)\|SEAWATER OUTLET(26,5)\|CARBON DIOXIDE GAS(25,33)\|LIQUID CLARIFICATION(25,12)\|REBOILER(25,10)\|LEAN LIQUID INLET(25,6)\|RICH LIQUID HEAT EXCHANGER(25,6)\|TREATING FLUE GAS(25,2)\|LEAN LIQUID PUMP(24,9)\|TRANSPORTATION(24,8)\|LIQUEFACTION(24,3)\|CARBON DIOXIDE ESCAPE(24,2)\|CARBON FIXATION(23,11)\|SOLUBLE CALCIUM BICARBONATE(23,7)\|CARBON DIOXIDE GAS SALIFYING(23,2)\|FLUE GAS(22,22)\|LIQUID CIRCULATION(22,6)\|FIXED CARBON FIXATION(22,1)\|LEAN RICH SOLUTION(22,1)\|RICH LIQUID PUMP(21,11)\|RICH LIQUID INLET(21,6)\|LEAN LIQUID OUTLET(21,3)\|ROCK REINFORCEMENT(21,3)\|LARGE MANPOWER(21,2)\|GAS OUTLET(20,10)\|CARBON FIXING(20,6)\|CALCIUM BICARBONATE(19,14)\|MIXER(19,12)\|LIMESTONE(19,7)\|BOOSTER FAN(19,3)\|RICH LIQUID OUTLET(19,3)\|DECARBURIZATION TREATMENT(19,2)\|LEAN SOLUTION COOLER(19,2)\|CONSUMPTION EQUIPMENT(19,1)\|ACIDIC CONDITION(18,6)\|SLAG DISCHARGE PUMP(18,4)\|EQUIPMENT RESOURCE CONSUMPTION(18,3)\|LEAN(18,2)\|DEEP SEA DISCHARGE AREA(17,8)\|SALTY WATER LAYER SEALING(17,2)\|SEALING FLOW(17,2)\|WATER FLOW PIPELINE(16,6)\|HEAT EXCHANGER(15,26)\|LIMESTONE SLURRY PUMP(15,6)\|ORGANIC AMINE(15,4)\|TRANSPORTATION(15,3)\|STEAM ABSORPTION HEAT(14,3)\|CARBON FIXATION COST(14,1)\|BYPASS VALVE(13,8)\|DISCHARGE AREA(13,8)\|SUPERFINE LIMESTONE POWDER(13,3)\|FLUE GAS SOURCE(12,6)\|EXHAUST GAS(12,5)\|CARBONIZATION TANK TOP(12,3)\|DISCHARGE OUTLET(12,3)\|CARBON CAPTURE SEALING(12,2)\|EQUIPMENT RESOURCE(12,1)\|WATER OUTLET(11,6)\|BIN(11,4)\|ENERGY CONSUMPTION(11,3)\|LIQUID HEAT EXCHANGER(11,2)\|WASTE GAS(10,25)\|TEMPERATURE REDUCTION TOWER BOTTOM(10,7)\|EXHAUST PORT(10,4)\|AIRFLOW PIPELINE(10,3)\|CARBON DIOXIDE CARBON FIXING(10,1)\|CARBON FIXING COST(10,1)\|STIRRER(9,7)\|HIGH ENERGY CONSUMPTION(9,3)\|SLURRY CONVEYING PIPELINE(9,2)\|CONVEYING LIMESTONE SLURRY SLAG(9,1)\|SEALING(9,1)\|GENERATED CALCIUM BICARBONATE(8,3)\|COMPRESSOR BOOSTER REFRIGERATOR(8,1)\|MIXED LIQUID(7,6)\|AIR FLOW PIPELINE(7,3)\|DESLAGGING PUMP(7,3)\|PH VALUE(7,2)\|WASTE GAS ABSORPTION UNIT(7,2)\|LIMESTONE POWDER WAREHOUSE(7,1)\|ABSORPTION UNIT(6,2)\|LIMESTONE SEDIMENT(6,1)\|TRIETHYLENE TETRAMINE(6,1)\|MIXER UPPER END(5,3)\|SEAWATER SPRAY(5,1)\|FORMED RICH AMINE LIQUID(4,3)\|BICARBONATE ION(4,2)\|FORMED LEAN AMINE SOLUTION(4,2)\|INPUT END(4,2)\|LEAN AMINE LIQUID SPRAY(4,1)\|SIMULTANEOUSLY CONVEYING LIMESTONE POWDER(4,1)\|AIR OUTLET(3,5)\|CLEAN GAS(3,2)\|DECARBONIZATION(3,2)\|OUTPUT END(3,2)\|ABSORPTION CARBON(3,1)\|CARBON DIOXIDE ESCAPING PHENOMENON(3,1)\|	(CN119607861)\|1. The carbon capturing and storing system is characterized by comprising an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit, a carbon fixation and sealing unit and a limestone slurry pulping and filling unit;\| The waste gas absorption unit comprises a temperature reduction tower and an absorption tower, wherein the upper part of the temperature reduction tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reduction tower is communicated with the absorption tower, a seawater spraying device is arranged in the temperature reduction tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reduction tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through a water conveying pipeline, the bottom of the temperature reduction tower is also provided with a seawater outlet, the upper end in the absorption tower is provided with a lean amine liquid spraying device, and the top of the absorption tower is provided with an exhaust port; \| The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; \| The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; \| The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; \| The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. \|2. The carbon capture and storage system of claim 1, wherein the bottom of the temperature reduction tower is communicated with the bottom of the absorption tower through an air flow pipeline, and a booster fan is arranged on the air flow pipeline between the temperature reduction tower and the absorption tower.\|3. The carbon capture storage system of claim 2, wherein the amine liquid circulation unit further comprises a rich liquid pump and a lean liquid pump, wherein an input end of the rich liquid pump is communicated with the bottom of the absorption tower, an output end of the rich liquid pump is communicated with a rich liquid inlet of the lean-rich liquid heat exchanger, an input end of the lean liquid pump is communicated with the bottom of the desorption tower, and an output end of the lean liquid pump is communicated with a lean liquid inlet of the lean-rich liquid heat exchanger.\|4. A carbon capture storage system according to claim 2, wherein a pressure relief valve is disposed in the gas flow line between the gas outlet and the compressor.\|5. The carbon capture and storage system according to claim 2, wherein a bubble distributor and a stirrer are arranged in the carbonization tank, and the bubble distributor is communicated with the output end of the compressor.\|6. A carbon capture storage system according to claim 2 wherein the bottom of the filter is in communication with a limestone slurry pond, the upper end of the filter is further provided with a gas outlet, and the gas outlet is in communication with the input of the compressor via a gas flow line.\|7. A carbon capture storage method, characterized in that the carbon capture storage system according to any one of claims 1 to 6 is used for carbon capture storage, comprising the steps of:\| S1, when waste gas needs decarburization treatment, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, the temperature is reduced to 40-60 ℃, the waste gas flows into the absorption tower from the bottom of the absorption tower, contacts with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, so that rich amine liquid and relatively pure gas are formed, and the relatively pure gas flows out from a gas outlet; \| S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid from the top of the desorption tower to the bottom of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a reboiler, desorbing carbon dioxide gas and forming lean amine liquid; \| S3, forming lean amine liquid, cooling the lean amine liquid twice through a lean-rich liquid heat exchanger and a lean liquid cooler, conveying the lean amine liquid to the top in an absorption tower, simultaneously, cooling the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing the cooled lean amine liquid to 4-6bar through a compressor, conveying the cooled lean amine liquid to the bottom of a carbonization tank, then, reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition based on a reinforced rock weathering principle to generate soluble calcium bicarbonate, conveying part of unreacted carbon dioxide gas to the compressor from an air outlet at the top of the carbonization tank, and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again; \| S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter for filtering to form clarified liquid and limestone slurry slag, conveying limestone powder and seawater into a limestone slurry tank to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank; \| s5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater in proportion to form mixed liquid with a pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, and conveying limestone slurry residues in the filter into a limestone slurry tank for preparing limestone slurry. \|8. The carbon capture storage method of claim 7, wherein in S2, the twice cooling of the formed lean amine solution comprises cooling to 60-70 ℃ by a lean rich solution heat exchanger and cooling to 30-45 ℃ by a lean solution cooler.\|9. The carbon capture storage method of claim 7, wherein in S5 the ratio of clarified liquid to seawater is 1 (10-1000).	(CN119607861)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of flue gas treatment, in particular to a carbon capture storage system and a carbon capture storage method.\|BACKGROUND ART\|[0002] The carbon dioxide discharged by the large amount of fossil fuels is a main cause of global warming, the carbon dioxide discharged is captured, utilized and sealed, and is one of the most effective means for realizing large-scale carbon emission reduction and coping with climate change, and at present, the carbon dioxide is captured by adopting a chemical absorption carbon capturing technology after the fossil fuels are combusted.\|[0003] The method for decarbonizing and storing the organic amine is one of the most main carbon trapping technologies by a chemical absorption method, and the existing method for decarbonizing and storing the organic amine is a method for capturing and storing the carbon dioxide from the waste gas by utilizing the principle that an organic amine is in contact with the carbon-containing waste gas and is subjected to absorption reaction and then rich liquid is heated and reversibly desorbed, then the carbon dioxide is stored in a liquid tank by utilizing a method of cooling and liquefying a compressor booster refrigerator, and the liquid carbon dioxide is conveyed to underground capable of being permanently stored by transportation, so that the purpose of capturing and storing the carbon dioxide is achieved.\|[0004] In the process of capturing and sealing carbon dioxide by adopting the organic amine decarburization storage method, a large amount of energy is consumed in the processes of compressing, liquefying, storing, transporting, sealing and the like of the carbon dioxide, at least 300KWh of energy is consumed per ton of compressed, liquefied and stored carbon dioxide, and in addition, the carbon dioxide is sealed in a low-temperature, high-pressure storage and high-pressure saline water layer sealing mode, so that the capturing and sealing process of the method is longer, the carbon dioxide is required to be ensured to be in a liquid state during the capturing and sealing process, and high energy is required to be consumed for keeping the liquid state of the carbon dioxide.\|[0005] The invention provides a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|DISCLOSURE\|Disclosure of Invention\|[0006] The invention aims to provide a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|[0007] The technical scheme includes that the carbon capturing and storing system comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salifying unit, a carbon fixing and sealing unit and a limestone slurry pulping and filling unit, wherein the exhaust gas absorbing unit comprises a temperature reducing tower and an absorbing tower, the upper part of the temperature reducing tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reducing tower is communicated with the absorbing tower, a seawater spraying device is arranged in the temperature reducing tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reducing tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through the water conveying pipeline, the bottom of the temperature reducing tower is also provided with a seawater outlet, the upper end of the inside of the absorbing tower is provided with a lean amine liquid spraying device, and the top of the absorbing tower is provided with an exhaust port;\| The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; \| The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; \| The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; \| The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. \|[0008] Preferably, the bottom of the temperature reduction tower is communicated with the bottom of the absorption tower through an airflow pipeline, and a booster fan is arranged on the airflow pipeline between the temperature reduction tower and the absorption tower.\|[0009] Preferably, the amine liquid circulation unit further comprises a rich liquid pump and a lean liquid pump, wherein the input end of the rich liquid pump is communicated with the bottom of the absorption tower, the output end of the rich liquid pump is communicated with a rich liquid inlet of the lean-rich liquid heat exchanger, the input end of the lean liquid pump is communicated with the bottom of the desorption tower, and the output end of the lean liquid pump is communicated with a lean liquid inlet of the lean-rich liquid heat exchanger.\|[0010] Preferably, a pressure reducing valve is arranged on the air flow pipeline between the air outlet and the compressor.\|[0011] Preferably, a bubble distributor and a stirrer are arranged in the carbonization tank, and the bubble distributor is communicated with the output end of the compressor.\|[0012] Preferably, the bottom of the filter is communicated with the limestone slurry pond, the upper end of the filter is also provided with a gas outlet, and the gas outlet is communicated with the input end of the compressor through a gas flow pipeline.\|[0013] The invention also provides a method for capturing and storing carbon by adopting the carbon capturing and storing system, which specifically comprises the following steps:\| S1, when waste gas needs decarburization treatment, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, the temperature is reduced to 40-60 ℃, the waste gas flows into the absorption tower from the bottom of the absorption tower, contacts with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, so that rich amine liquid and relatively pure gas are formed, and the relatively pure gas flows out from a gas outlet; \| S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid from the top of the desorption tower to the bottom of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a reboiler, desorbing carbon dioxide gas and forming lean amine liquid; \| S3, forming lean amine liquid, cooling the lean amine liquid twice through a lean-rich liquid heat exchanger and a lean liquid cooler, conveying the lean amine liquid to the top in an absorption tower, simultaneously, cooling the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing the cooled lean amine liquid to 4-6bar through a compressor, conveying the cooled lean amine liquid to the bottom of a carbonization tank, then, reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition based on a reinforced rock weathering principle to generate soluble calcium bicarbonate, conveying part of unreacted carbon dioxide gas to the compressor from an air outlet at the top of the carbonization tank, and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again; \| S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter for filtering to form clarified liquid and limestone slurry slag, conveying limestone powder and seawater into a limestone slurry tank to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank; \| s5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater in proportion to form mixed liquid with a pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, and conveying limestone slurry residues in the filter into a limestone slurry tank for preparing limestone slurry. \|[0014] Preferably, in S2, the two cooling steps of the formed lean amine solution include cooling to 60-70 ℃ by a lean-rich solution heat exchanger and cooling to 30-45 ℃ by a lean solution cooler.\|[0015] Preferably, in S5, the ratio of clarified liquid to seawater is 1 (10-1000).\|[0016] Compared with the prior art, the invention has the advantages that:\| (1) The invention provides a carbon capture storage system and a carbon capture storage method, wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine, then resolving the carbon dioxide gas in a desorption tower, then reacting the resolved carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, and finally sealing the calcium bicarbonate in a deep sea discharge area; compared with the traditional carbon fixation method of carbon dioxide through compression, liquefaction and transportation and underground salty water layer sealing, the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short, high-pressure and low-temperature high-energy equipment is not needed in the carbon capture and sealing process, the low-temperature storage and transportation of captured carbon dioxide gas are not needed, the energy consumption can be reduced, the carbon fixation cost can be saved, the phenomenon of carbon dioxide escape in the storage and transportation process can be avoided, the carbon fixation efficiency is improved, meanwhile, the consumption in the aspects of manpower and material resources can be reduced, and the problems of overlong carbon capture and sealing flow, high energy consumption, high cost, high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved. \|[0017] (2) The carbon capture storage system and the carbon capture storage method provided by the invention are characterized in that the carbon capture storage method is used for converting the resolved carbon dioxide gas and limestone slurry into calcium bicarbonate under an acidic condition, and the calcium bicarbonate can exist stably in the form of bicarbonate ions and calcium ions under deep sea and low temperature conditions, so that the carbon capture storage method can realize the purpose of permanently fixing carbon.\|DRAWINGS DESCRIPTION\|[0018] The invention is further described below with reference to the accompanying drawings and examples:\| FIG. 1 is a schematic diagram of a carbon capture storage system according to the present invention; \| The device comprises a temperature reduction tower, a2 absorption tower, a3 bypass valve, a 4 sea water pump, a 5 sea water outlet, a 6, an exhaust port, a7, a desorption tower, a 8, a lean-rich liquid heat exchanger, a9, a reboiler, a 10, a lean liquid cooler, a 11, a regenerated gas cooler, a 12, a compressor, a 13, a carbonization tank, a 14, an air outlet, a 15, a slag discharge pump, a 16, a filter, a 17, a mixer, a 18, a water outlet, a 19, a PH meter, a 20, a limestone slurry pond, a 21, a limestone powder warehouse, a 22, a booster fan, a 23, a rich liquid pump, a 24, a lean liquid pump, a 25, a pressure reducing valve, a 26, a bubble distributor, a 27, a stirrer, a 28, a gas outlet, a 29 and a limestone slurry pump. \|INVENTION MODE\|Detailed Description\|[0019] The following describes the present invention in further detail with reference to specific examples:\| A carbon capturing and storing system is shown in fig. 1, and comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit and a carbon fixation and sealing unit which are sequentially communicated, wherein the carbon capturing and storing system also comprises a limestone slurry pulping and filling unit, and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. \|[0020] The waste gas absorption unit comprises a temperature reduction tower 1 and an absorption tower 2; the upper part of the temperature reduction tower 1 is communicated with a flue gas source through a flue gas conveying pipeline, and a bypass valve 3 is arranged on the flue gas conveying pipeline between the temperature reduction tower 1 and the flue gas source; the bypass valve 3 is opened to convey the waste gas to be decarbonized into the temperature reduction tower 1 for cooling treatment, a seawater spray device is arranged at the upper end of the interior of the temperature reduction tower 1, the seawater spray device is connected with the output end of a seawater pump 4 positioned outside the temperature reduction tower 1 through a water pipeline, the seawater is conveyed into the temperature reduction tower 1, the upper end of the temperature reduction tower 1 sprays the waste gas to the bottom of the temperature reduction tower 1 and fully contacts and mixes the waste gas conveyed into the temperature reduction tower 1 to further reduce the temperature of the waste gas, the bottom of the temperature reduction tower 1 is communicated with the absorption tower 2 and is used for conveying the waste gas subjected to the spray cooling treatment into the absorption tower 2, a seawater outlet 5 is also arranged at the bottom of the temperature reduction tower 1, a water pipeline leading to a seawater discharge area is connected at the seawater outlet 5 and is used for discharging the seawater sprayed to the bottom of the temperature reduction tower 1 into the sea, a lean amine liquid spray device is arranged at the upper end of the absorption tower 2 and is used for spraying the lean amine liquid from the upper end of the absorption tower 2 to a filler position close to the bottom of the absorption tower 2 and is fully contacted with the waste gas conveyed into the absorption tower 2, the waste gas is further reduced in temperature, the bottom of the absorption tower 2 is in contact with the waste gas is formed by the pure amine gas and the pure amine gas is discharged into the absorption tower 2 through the clean gas after the absorption tower 2 is relatively connected to the top of the absorption tower 2 through the clean gas which is relatively arranged to the top of the absorption tower 2, and the booster fan 22 is further arranged on the airflow pipeline between the temperature reduction tower 1 and the absorption tower 2 and is used for increasing the pressure of the waste gas conveyed into the absorption tower 2, increasing the flow speed and the airflow energy of the waste gas, and fully mixing the waste gas with the lean amine liquid in the absorption tower 2, so that the carbon dioxide gas in the waste gas fully contacts with the lean amine liquid and is absorbed by the lean amine liquid, and capturing the carbon dioxide gas in the waste gas is realized.\|[0021] The amine liquid circulation unit comprises a desorption tower 7, a lean-rich liquid heat exchanger 8 and a reboiler 9, wherein the reboiler 9 is communicated with the desorption tower 7 and is connected to a position close to the bottom of the desorption tower 7, namely a filler, a rich liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the absorption tower 2, a rich liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the desorption tower 7 and is used for heating the rich amine liquid at the bottom of the absorption tower 2 and then conveying the rich amine liquid to the top of the desorption tower 7, a spraying device at the top of the desorption tower 7 is used for spraying the rich amine liquid close to the bottom of the desorption tower 7 from the top of the desorption tower 7, the rich amine liquid sprayed to the filler absorbs steam heat generated by the reboiler 9 and then heats and desorbs carbon dioxide to form lean amine liquid containing only a small amount of carbon dioxide, and flows to the bottom of the desorption tower 7, a lean liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the desorption tower 7, a lean liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the absorption tower 2 through a lean liquid cooler 10 and is used for cooling the lean liquid at the bottom of the absorption tower 2, and is conveyed to the top of the absorption tower 2 from the lean liquid heat exchanger 8 to the top of the absorption tower 2 through the lean liquid heat exchanger 10 and then is recycled to the absorption tower 2. In order to ensure continuous and stable mutual circulation and transportation of the rich amine liquid and the lean amine liquid formed in the absorption tower 2 and the desorption tower 7 so as to achieve the effect of recycling the organic amine liquid, the amine liquid circulation unit further comprises a rich liquid pump 23 and a lean liquid pump 24, wherein the input end of the rich liquid pump 23 is communicated with the bottom of the absorption tower 2, the output end of the rich liquid pump is communicated with the rich liquid inlet of the lean-rich liquid heat exchanger 8 and is used for pumping the rich amine liquid formed in the absorption tower 2 into the lean-rich liquid heat exchanger 8 and transporting the rich amine liquid into the desorption tower 7, and similarly, the input end of the lean liquid pump 24 is communicated with the bottom of the desorption tower 7, and the output end of the rich liquid pump 24 is communicated with the lean liquid inlet of the lean-rich liquid heat exchanger 8.\|[0022] The carbon dioxide gas salinization unit comprises a regeneration gas cooler 11, a compressor 12 and a carbonization tank 13, wherein the input end of the regeneration gas cooler 11 is communicated with the top of the desorption tower 7, the output end of the regeneration gas cooler is communicated with the input end of the compressor 12, the output end of the compressor 12 is communicated with the bottom of the carbonization tank 13, carbon dioxide gas desorbed in the desorption tower 7 is cooled by the regeneration gas cooler 11, dehydrated and then flows into the compressor 12, the compressor 12 is pressurized and then is conveyed into the carbonization tank 13, and based on the rock weathering principle, the carbon dioxide gas and limestone slurry in the carbonization tank 13 are mixed and react under the acidic condition to form soluble calcium bicarbonate. In order to sufficiently mix and sufficiently react the carbon dioxide gas with the limestone slurry in the carbonization tank 13, a bubble distributor 26 and a stirrer 27 may be provided in the carbonization tank 13, the bubble distributor 26 may be connected to the output end of the compressor 12, the carbon dioxide gas supplied into the carbonization tank 13 by the compressor 12 may be separated into fine bubbles by the bubble distributor 26, the dissolution efficiency of the carbon dioxide gas in the limestone slurry may be improved, the contact ratio of the carbon dioxide gas with the limestone slurry may be increased, and the reaction efficiency may be improved, and the carbon dioxide gas and the limestone slurry in the carbonization tank 13 may be sufficiently mixed and reacted with each other by stirring by the stirrer 27, thereby further improving the conversion rate of the carbon dioxide.\|[0023] The carbon sequestration unit comprises a deslagging pump 15, a filter 16 and a mixer 17, wherein the input end of the deslagging pump 15 is communicated with the bottom of the carbonization tank 13, the output end of the deslagging pump 15 is communicated with the filter 16 and is used for conveying soluble calcium bicarbonate and limestone slurry generated by the reaction at the bottom of the carbonization tank 13 into the filter 16 together for filtering, the upper end of the filter 16 is communicated with the mixer 17, the upper end of the mixer 17 is communicated with the output end of the sea water pump 4 through a water flow pipeline, the lower end of the mixer 17 is provided with a water outlet 18, the water outlet 18 is communicated with a water flow pipeline leading to a deep sea discharge area, the clarified liquid separated from the filter 16 is conveyed into the mixer 17 and is mixed with sea water from the sea water pump 4 in the mixer 17 to form mixed liquid, then the mixed liquid is discharged into the deep sea discharge area through the water flow pipeline to achieve the purpose of permanently sequestration, and a PH meter 19 is further arranged at the water outlet 18 and is used for monitoring the PH value of the mixed liquid and the sea water, and the clear liquid is discharged into the deep sea after the PH value of the clear liquid meets the requirements. The upper end of the filter 16 is also provided with a gas outlet 28, and the gas outlet 28 is communicated with the input end of the compressor 12 through a gas flow pipeline and is used for conveying the carbon dioxide gas which is conveyed into the filter 16 together with the soluble calcium bicarbonate and limestone slurry into a carbon dioxide gas salinization unit for continuous salinization.\|[0024] The limestone slurry pulping and filling unit comprises a limestone slurry pond 20, wherein the upper part of the limestone slurry pond 20 is respectively communicated with a limestone powder bin 21 and the output end of a sea water pump 4, and is used for adding superfine limestone powder and sea water in the limestone powder bin 21 into the limestone slurry pond 20 together and uniformly mixing the superfine limestone powder and the sea water in the limestone slurry pond 20 to form limestone slurry, a stirrer 27 is further arranged in the limestone slurry pond 20, stirring is performed by adopting the stirrer 27 in the process of adding the limestone powder and the sea water into the limestone slurry pond 20, so that rapid uniform mixing of the limestone powder and the sea water is facilitated, the bottom of the limestone slurry pond 20 is communicated with the upper part of a carbonization tank 13 through a slurry conveying pipeline, a limestone slurry pump 29 is arranged on the slurry conveying pipeline, and the limestone slurry in the limestone slurry pond 20 is pumped into the carbonization tank 13 through the limestone slurry pump 29 to perform internal reaction. The bottom of the filter 16 is also communicated with the limestone slurry pond 20, and limestone sediment formed at the lower layer in the filter 16 is conveyed into the limestone slurry pond 20 and is used as a raw material together with superfine limestone powder to prepare limestone slurry.\|[0025] The method for capturing and storing carbon by adopting the carbon capturing and storing system specifically comprises the following steps:\| S1, when the waste gas needs to be decarbonized, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, seawater sprayed through a Wen Dana is fully contacted with the flue gas and absorbs heat brought by the flue gas, so that the flue gas is cooled to be within a range of 40-60 ℃, then, the waste gas flows into the absorption tower from the bottom of the absorption tower, is contacted with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, rich amine liquid and relatively pure gas are formed, and the relatively pure gas is discharged into the atmosphere from an exhaust port at the top of the absorption tower or is conveyed to a subsequent gas treatment unit. Wherein, the flue gas is conveyed into a temperature reduction tower according to the gas flow of 50-500L/h, the lean amine liquid in the absorption tower can be one of aqueous solution or mixed aqueous solution of a plurality of methyl diethanolamine, ethanolamine, triethylene tetramine and the like, and the concentration of carbon dioxide gas in the relatively pure gas is below 2.0 percent (mole percent). \|[0026] S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid to the bottom from the top of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a bottom reboiler, desorbing carbon dioxide gas, forming lean amine liquid, and flowing to the bottom of the desorption tower.\|[0027] S3, cooling the lean amine liquid at the bottom of the desorption tower to 60-70 ℃ through a lean-rich liquid heat exchanger, cooling to 30-45 ℃ through a lean liquid cooler, conveying the lean amine liquid to the top of the absorption tower, spraying the lean amine liquid to the bottom of the absorption tower from the top in the absorption tower, simultaneously, cooling and dewatering the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing to 4-6bar through a compressor, and conveying the carbon dioxide gas to the bottom of a carbonization tank, and then, based on the reinforced rock weathering principle, absorbing and reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, wherein the reaction equation is as follows: And conveying part of unreacted carbon dioxide gas to a compressor from an air outlet at the top of the carbonization tank, compressing and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again. \|[0028] S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter according to the flow ratio of 5-100L/h for filtering to form clarified liquid and limestone slurry slag, simultaneously conveying limestone powder and seawater into a limestone slurry pond to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank according to the flow ratio of 5-100L/h.\|[0029] S5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater according to the proportion of 1 (10-1000), forming mixed liquid with the pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, achieving the purpose of carbon fixation and sealing, and conveying limestone slurry slag in the filter into a limestone slurry pond for preparing limestone slurry.\|[0030] Compared with the traditional carbon fixation method for sealing and storing carbon dioxide through compression, liquefaction and transportation and an underground salty water layer, the carbon capture and storage method does not need high-pressure and low-temperature high-energy equipment, low-temperature storage and transportation, saves the cost consumed in the low-temperature storage, transportation and sealing and storage processes, avoids the carbon dioxide escaping phenomenon in the transportation process, greatly shortens the carbon fixation process, and reduces the carbon fixation energy consumption. In addition, because the calcium bicarbonate exists in the form of bicarbonate ions and calcium ions in the sea water and can exist stably under deep sea and low temperature conditions, the carbon capturing and storing method can better achieve the purpose of carbon fixation and sealing.\|[0031] The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and implement the same according to the content of the present invention, and are not intended to limit the scope of the present invention. It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof, and it is therefore desired that the present invention be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.	(CN119607861)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of flue gas treatment, in particular to a carbon capture storage system and a carbon capture storage method.\|BACKGROUND ART\|[0002] The carbon dioxide discharged by the large amount of fossil fuels is a main cause of global warming, the carbon dioxide discharged is captured, utilized and sealed, and is one of the most effective means for realizing large-scale carbon emission reduction and coping with climate change, and at present, the carbon dioxide is captured by adopting a chemical absorption carbon capturing technology after the fossil fuels are combusted.\|[0003] The method for decarbonizing and storing the organic amine is one of the most main carbon trapping technologies by a chemical absorption method, and the existing method for decarbonizing and storing the organic amine is a method for capturing and storing the carbon dioxide from the waste gas by utilizing the principle that an organic amine is in contact with the carbon-containing waste gas and is subjected to absorption reaction and then rich liquid is heated and reversibly desorbed, then the carbon dioxide is stored in a liquid tank by utilizing a method of cooling and liquefying a compressor booster refrigerator, and the liquid carbon dioxide is conveyed to underground capable of being permanently stored by transportation, so that the purpose of capturing and storing the carbon dioxide is achieved.\|[0004] In the process of capturing and sealing carbon dioxide by adopting the organic amine decarburization storage method, a large amount of energy is consumed in the processes of compressing, liquefying, storing, transporting, sealing and the like of the carbon dioxide, at least 300KWh of energy is consumed per ton of compressed, liquefied and stored carbon dioxide, and in addition, the carbon dioxide is sealed in a low-temperature, high-pressure storage and high-pressure saline water layer sealing mode, so that the capturing and sealing process of the method is longer, the carbon dioxide is required to be ensured to be in a liquid state during the capturing and sealing process, and high energy is required to be consumed for keeping the liquid state of the carbon dioxide.\|[0005] The invention provides a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|DISCLOSURE\|Disclosure of Invention\|[0006] The invention aims to provide a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|[0007] The technical scheme includes that the carbon capturing and storing system comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salifying unit, a carbon fixing and sealing unit and a limestone slurry pulping and filling unit, wherein the exhaust gas absorbing unit comprises a temperature reducing tower and an absorbing tower, the upper part of the temperature reducing tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reducing tower is communicated with the absorbing tower, a seawater spraying device is arranged in the temperature reducing tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reducing tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through the water conveying pipeline, the bottom of the temperature reducing tower is also provided with a seawater outlet, the upper end of the inside of the absorbing tower is provided with a lean amine liquid spraying device, and the top of the absorbing tower is provided with an exhaust port;\| The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; \| The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; \| The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; \| The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. \|[0008] Preferably, the bottom of the temperature reduction tower is communicated with the bottom of the absorption tower through an airflow pipeline, and a booster fan is arranged on the airflow pipeline between the temperature reduction tower and the absorption tower.\|[0009] Preferably, the amine liquid circulation unit further comprises a rich liquid pump and a lean liquid pump, wherein the input end of the rich liquid pump is communicated with the bottom of the absorption tower, the output end of the rich liquid pump is communicated with a rich liquid inlet of the lean-rich liquid heat exchanger, the input end of the lean liquid pump is communicated with the bottom of the desorption tower, and the output end of the lean liquid pump is communicated with a lean liquid inlet of the lean-rich liquid heat exchanger.\|[0010] Preferably, a pressure reducing valve is arranged on the air flow pipeline between the air outlet and the compressor.\|[0011] Preferably, a bubble distributor and a stirrer are arranged in the carbonization tank, and the bubble distributor is communicated with the output end of the compressor.\|[0012] Preferably, the bottom of the filter is communicated with the limestone slurry pond, the upper end of the filter is also provided with a gas outlet, and the gas outlet is communicated with the input end of the compressor through a gas flow pipeline.\|[0013] The invention also provides a method for capturing and storing carbon by adopting the carbon capturing and storing system, which specifically comprises the following steps:\| S1, when waste gas needs decarburization treatment, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, the temperature is reduced to 40-60 ℃, the waste gas flows into the absorption tower from the bottom of the absorption tower, contacts with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, so that rich amine liquid and relatively pure gas are formed, and the relatively pure gas flows out from a gas outlet; \| S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid from the top of the desorption tower to the bottom of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a reboiler, desorbing carbon dioxide gas and forming lean amine liquid; \| S3, forming lean amine liquid, cooling the lean amine liquid twice through a lean-rich liquid heat exchanger and a lean liquid cooler, conveying the lean amine liquid to the top in an absorption tower, simultaneously, cooling the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing the cooled lean amine liquid to 4-6bar through a compressor, conveying the cooled lean amine liquid to the bottom of a carbonization tank, then, reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition based on a reinforced rock weathering principle to generate soluble calcium bicarbonate, conveying part of unreacted carbon dioxide gas to the compressor from an air outlet at the top of the carbonization tank, and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again; \| S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter for filtering to form clarified liquid and limestone slurry slag, conveying limestone powder and seawater into a limestone slurry tank to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank; \| s5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater in proportion to form mixed liquid with a pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, and conveying limestone slurry residues in the filter into a limestone slurry tank for preparing limestone slurry. \|[0014] Preferably, in S2, the two cooling steps of the formed lean amine solution include cooling to 60-70 ℃ by a lean-rich solution heat exchanger and cooling to 30-45 ℃ by a lean solution cooler.\|[0015] Preferably, in S5, the ratio of clarified liquid to seawater is 1 (10-1000).\|[0016] Compared with the prior art, the invention has the advantages that:\| (1) The invention provides a carbon capture storage system and a carbon capture storage method, wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine, then resolving the carbon dioxide gas in a desorption tower, then reacting the resolved carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, and finally sealing the calcium bicarbonate in a deep sea discharge area; compared with the traditional carbon fixation method of carbon dioxide through compression, liquefaction and transportation and underground salty water layer sealing, the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short, high-pressure and low-temperature high-energy equipment is not needed in the carbon capture and sealing process, the low-temperature storage and transportation of captured carbon dioxide gas are not needed, the energy consumption can be reduced, the carbon fixation cost can be saved, the phenomenon of carbon dioxide escape in the storage and transportation process can be avoided, the carbon fixation efficiency is improved, meanwhile, the consumption in the aspects of manpower and material resources can be reduced, and the problems of overlong carbon capture and sealing flow, high energy consumption, high cost, high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved. \|[0017] (2) The carbon capture storage system and the carbon capture storage method provided by the invention are characterized in that the carbon capture storage method is used for converting the resolved carbon dioxide gas and limestone slurry into calcium bicarbonate under an acidic condition, and the calcium bicarbonate can exist stably in the form of bicarbonate ions and calcium ions under deep sea and low temperature conditions, so that the carbon capture storage method can realize the purpose of permanently fixing carbon.\|DRAWINGS DESCRIPTION\|[0018] The invention is further described below with reference to the accompanying drawings and examples:\| FIG. 1 is a schematic diagram of a carbon capture storage system according to the present invention; \| The device comprises a temperature reduction tower, a2 absorption tower, a3 bypass valve, a 4 sea water pump, a 5 sea water outlet, a 6, an exhaust port, a7, a desorption tower, a 8, a lean-rich liquid heat exchanger, a9, a reboiler, a 10, a lean liquid cooler, a 11, a regenerated gas cooler, a 12, a compressor, a 13, a carbonization tank, a 14, an air outlet, a 15, a slag discharge pump, a 16, a filter, a 17, a mixer, a 18, a water outlet, a 19, a PH meter, a 20, a limestone slurry pond, a 21, a limestone powder warehouse, a 22, a booster fan, a 23, a rich liquid pump, a 24, a lean liquid pump, a 25, a pressure reducing valve, a 26, a bubble distributor, a 27, a stirrer, a 28, a gas outlet, a 29 and a limestone slurry pump. \|INVENTION MODE\|Detailed Description\|[0019] The following describes the present invention in further detail with reference to specific examples:\| A carbon capturing and storing system is shown in fig. 1, and comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit and a carbon fixation and sealing unit which are sequentially communicated, wherein the carbon capturing and storing system also comprises a limestone slurry pulping and filling unit, and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. \|[0020] The waste gas absorption unit comprises a temperature reduction tower 1 and an absorption tower 2; the upper part of the temperature reduction tower 1 is communicated with a flue gas source through a flue gas conveying pipeline, and a bypass valve 3 is arranged on the flue gas conveying pipeline between the temperature reduction tower 1 and the flue gas source; the bypass valve 3 is opened to convey the waste gas to be decarbonized into the temperature reduction tower 1 for cooling treatment, a seawater spray device is arranged at the upper end of the interior of the temperature reduction tower 1, the seawater spray device is connected with the output end of a seawater pump 4 positioned outside the temperature reduction tower 1 through a water pipeline, the seawater is conveyed into the temperature reduction tower 1, the upper end of the temperature reduction tower 1 sprays the waste gas to the bottom of the temperature reduction tower 1 and fully contacts and mixes the waste gas conveyed into the temperature reduction tower 1 to further reduce the temperature of the waste gas, the bottom of the temperature reduction tower 1 is communicated with the absorption tower 2 and is used for conveying the waste gas subjected to the spray cooling treatment into the absorption tower 2, a seawater outlet 5 is also arranged at the bottom of the temperature reduction tower 1, a water pipeline leading to a seawater discharge area is connected at the seawater outlet 5 and is used for discharging the seawater sprayed to the bottom of the temperature reduction tower 1 into the sea, a lean amine liquid spray device is arranged at the upper end of the absorption tower 2 and is used for spraying the lean amine liquid from the upper end of the absorption tower 2 to a filler position close to the bottom of the absorption tower 2 and is fully contacted with the waste gas conveyed into the absorption tower 2, the waste gas is further reduced in temperature, the bottom of the absorption tower 2 is in contact with the waste gas is formed by the pure amine gas and the pure amine gas is discharged into the absorption tower 2 through the clean gas after the absorption tower 2 is relatively connected to the top of the absorption tower 2 through the clean gas which is relatively arranged to the top of the absorption tower 2, and the booster fan 22 is further arranged on the airflow pipeline between the temperature reduction tower 1 and the absorption tower 2 and is used for increasing the pressure of the waste gas conveyed into the absorption tower 2, increasing the flow speed and the airflow energy of the waste gas, and fully mixing the waste gas with the lean amine liquid in the absorption tower 2, so that the carbon dioxide gas in the waste gas fully contacts with the lean amine liquid and is absorbed by the lean amine liquid, and capturing the carbon dioxide gas in the waste gas is realized.\|[0021] The amine liquid circulation unit comprises a desorption tower 7, a lean-rich liquid heat exchanger 8 and a reboiler 9, wherein the reboiler 9 is communicated with the desorption tower 7 and is connected to a position close to the bottom of the desorption tower 7, namely a filler, a rich liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the absorption tower 2, a rich liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the desorption tower 7 and is used for heating the rich amine liquid at the bottom of the absorption tower 2 and then conveying the rich amine liquid to the top of the desorption tower 7, a spraying device at the top of the desorption tower 7 is used for spraying the rich amine liquid close to the bottom of the desorption tower 7 from the top of the desorption tower 7, the rich amine liquid sprayed to the filler absorbs steam heat generated by the reboiler 9 and then heats and desorbs carbon dioxide to form lean amine liquid containing only a small amount of carbon dioxide, and flows to the bottom of the desorption tower 7, a lean liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the desorption tower 7, a lean liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the absorption tower 2 through a lean liquid cooler 10 and is used for cooling the lean liquid at the bottom of the absorption tower 2, and is conveyed to the top of the absorption tower 2 from the lean liquid heat exchanger 8 to the top of the absorption tower 2 through the lean liquid heat exchanger 10 and then is recycled to the absorption tower 2. In order to ensure continuous and stable mutual circulation and transportation of the rich amine liquid and the lean amine liquid formed in the absorption tower 2 and the desorption tower 7 so as to achieve the effect of recycling the organic amine liquid, the amine liquid circulation unit further comprises a rich liquid pump 23 and a lean liquid pump 24, wherein the input end of the rich liquid pump 23 is communicated with the bottom of the absorption tower 2, the output end of the rich liquid pump is communicated with the rich liquid inlet of the lean-rich liquid heat exchanger 8 and is used for pumping the rich amine liquid formed in the absorption tower 2 into the lean-rich liquid heat exchanger 8 and transporting the rich amine liquid into the desorption tower 7, and similarly, the input end of the lean liquid pump 24 is communicated with the bottom of the desorption tower 7, and the output end of the rich liquid pump 24 is communicated with the lean liquid inlet of the lean-rich liquid heat exchanger 8.\|[0022] The carbon dioxide gas salinization unit comprises a regeneration gas cooler 11, a compressor 12 and a carbonization tank 13, wherein the input end of the regeneration gas cooler 11 is communicated with the top of the desorption tower 7, the output end of the regeneration gas cooler is communicated with the input end of the compressor 12, the output end of the compressor 12 is communicated with the bottom of the carbonization tank 13, carbon dioxide gas desorbed in the desorption tower 7 is cooled by the regeneration gas cooler 11, dehydrated and then flows into the compressor 12, the compressor 12 is pressurized and then is conveyed into the carbonization tank 13, and based on the rock weathering principle, the carbon dioxide gas and limestone slurry in the carbonization tank 13 are mixed and react under the acidic condition to form soluble calcium bicarbonate. In order to sufficiently mix and sufficiently react the carbon dioxide gas with the limestone slurry in the carbonization tank 13, a bubble distributor 26 and a stirrer 27 may be provided in the carbonization tank 13, the bubble distributor 26 may be connected to the output end of the compressor 12, the carbon dioxide gas supplied into the carbonization tank 13 by the compressor 12 may be separated into fine bubbles by the bubble distributor 26, the dissolution efficiency of the carbon dioxide gas in the limestone slurry may be improved, the contact ratio of the carbon dioxide gas with the limestone slurry may be increased, and the reaction efficiency may be improved, and the carbon dioxide gas and the limestone slurry in the carbonization tank 13 may be sufficiently mixed and reacted with each other by stirring by the stirrer 27, thereby further improving the conversion rate of the carbon dioxide.\|[0023] The carbon sequestration unit comprises a deslagging pump 15, a filter 16 and a mixer 17, wherein the input end of the deslagging pump 15 is communicated with the bottom of the carbonization tank 13, the output end of the deslagging pump 15 is communicated with the filter 16 and is used for conveying soluble calcium bicarbonate and limestone slurry generated by the reaction at the bottom of the carbonization tank 13 into the filter 16 together for filtering, the upper end of the filter 16 is communicated with the mixer 17, the upper end of the mixer 17 is communicated with the output end of the sea water pump 4 through a water flow pipeline, the lower end of the mixer 17 is provided with a water outlet 18, the water outlet 18 is communicated with a water flow pipeline leading to a deep sea discharge area, the clarified liquid separated from the filter 16 is conveyed into the mixer 17 and is mixed with sea water from the sea water pump 4 in the mixer 17 to form mixed liquid, then the mixed liquid is discharged into the deep sea discharge area through the water flow pipeline to achieve the purpose of permanently sequestration, and a PH meter 19 is further arranged at the water outlet 18 and is used for monitoring the PH value of the mixed liquid and the sea water, and the clear liquid is discharged into the deep sea after the PH value of the clear liquid meets the requirements. The upper end of the filter 16 is also provided with a gas outlet 28, and the gas outlet 28 is communicated with the input end of the compressor 12 through a gas flow pipeline and is used for conveying the carbon dioxide gas which is conveyed into the filter 16 together with the soluble calcium bicarbonate and limestone slurry into a carbon dioxide gas salinization unit for continuous salinization.\|[0024] The limestone slurry pulping and filling unit comprises a limestone slurry pond 20, wherein the upper part of the limestone slurry pond 20 is respectively communicated with a limestone powder bin 21 and the output end of a sea water pump 4, and is used for adding superfine limestone powder and sea water in the limestone powder bin 21 into the limestone slurry pond 20 together and uniformly mixing the superfine limestone powder and the sea water in the limestone slurry pond 20 to form limestone slurry, a stirrer 27 is further arranged in the limestone slurry pond 20, stirring is performed by adopting the stirrer 27 in the process of adding the limestone powder and the sea water into the limestone slurry pond 20, so that rapid uniform mixing of the limestone powder and the sea water is facilitated, the bottom of the limestone slurry pond 20 is communicated with the upper part of a carbonization tank 13 through a slurry conveying pipeline, a limestone slurry pump 29 is arranged on the slurry conveying pipeline, and the limestone slurry in the limestone slurry pond 20 is pumped into the carbonization tank 13 through the limestone slurry pump 29 to perform internal reaction. The bottom of the filter 16 is also communicated with the limestone slurry pond 20, and limestone sediment formed at the lower layer in the filter 16 is conveyed into the limestone slurry pond 20 and is used as a raw material together with superfine limestone powder to prepare limestone slurry.\|[0025] The method for capturing and storing carbon by adopting the carbon capturing and storing system specifically comprises the following steps:\| S1, when the waste gas needs to be decarbonized, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, seawater sprayed through a Wen Dana is fully contacted with the flue gas and absorbs heat brought by the flue gas, so that the flue gas is cooled to be within a range of 40-60 ℃, then, the waste gas flows into the absorption tower from the bottom of the absorption tower, is contacted with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, rich amine liquid and relatively pure gas are formed, and the relatively pure gas is discharged into the atmosphere from an exhaust port at the top of the absorption tower or is conveyed to a subsequent gas treatment unit. Wherein, the flue gas is conveyed into a temperature reduction tower according to the gas flow of 50-500L/h, the lean amine liquid in the absorption tower can be one of aqueous solution or mixed aqueous solution of a plurality of methyl diethanolamine, ethanolamine, triethylene tetramine and the like, and the concentration of carbon dioxide gas in the relatively pure gas is below 2.0 percent (mole percent). \|[0026] S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid to the bottom from the top of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a bottom reboiler, desorbing carbon dioxide gas, forming lean amine liquid, and flowing to the bottom of the desorption tower.\|[0027] S3, cooling the lean amine liquid at the bottom of the desorption tower to 60-70 ℃ through a lean-rich liquid heat exchanger, cooling to 30-45 ℃ through a lean liquid cooler, conveying the lean amine liquid to the top of the absorption tower, spraying the lean amine liquid to the bottom of the absorption tower from the top in the absorption tower, simultaneously, cooling and dewatering the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing to 4-6bar through a compressor, and conveying the carbon dioxide gas to the bottom of a carbonization tank, and then, based on the reinforced rock weathering principle, absorbing and reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, wherein the reaction equation is as follows: And conveying part of unreacted carbon dioxide gas to a compressor from an air outlet at the top of the carbonization tank, compressing and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again. \|[0028] S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter according to the flow ratio of 5-100L/h for filtering to form clarified liquid and limestone slurry slag, simultaneously conveying limestone powder and seawater into a limestone slurry pond to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank according to the flow ratio of 5-100L/h.\|[0029] S5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater according to the proportion of 1 (10-1000), forming mixed liquid with the pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, achieving the purpose of carbon fixation and sealing, and conveying limestone slurry slag in the filter into a limestone slurry pond for preparing limestone slurry.\|[0030] Compared with the traditional carbon fixation method for sealing and storing carbon dioxide through compression, liquefaction and transportation and an underground salty water layer, the carbon capture and storage method does not need high-pressure and low-temperature high-energy equipment, low-temperature storage and transportation, saves the cost consumed in the low-temperature storage, transportation and sealing and storage processes, avoids the carbon dioxide escaping phenomenon in the transportation process, greatly shortens the carbon fixation process, and reduces the carbon fixation energy consumption. In addition, because the calcium bicarbonate exists in the form of bicarbonate ions and calcium ions in the sea water and can exist stably under deep sea and low temperature conditions, the carbon capturing and storing method can better achieve the purpose of carbon fixation and sealing.\|[0031] The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and implement the same according to the content of the present invention, and are not intended to limit the scope of the present invention. It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof, and it is therefore desired that the present invention be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.	Family Number\|(113778323)\|113778323\|Object of Invention\|(CN119607861 A)\|The invention provides a carbon capture storage system and a carbon capture storage method , which are used for solving the problems of overlong carbon capture sealing process , high energy consumption , high cost , large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art . Disclosure of InventionThe invention aims to provide a carbon capture storage system and a carbon capture storage method , which are used for solving the problems of overlong carbon capture sealing process , high energy consumption , high cost , large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art . \|The invention relates to the technical field of flue gas treatment , in particular to a carbon capture storage system and a carbon capture storage method . \|The invention relates to the technical field of flue gas treatment , in particular to a carbon capturing and storing system and a carbon capturing and storing method , comprising an exhaust gas absorbing unit , an amine liquid circulating unit , a carbon dioxide gas salifying unit and a carbon fixing and sealing unit which are sequentially communicated ; the device also comprises a limestone ( . . . ) \|Abstract\|(CN119607861 A)\|The invention relates to the technical field of flue gas treatment , in particular to a carbon capture and storage system and a carbon capture and storage method . The carbon capture and storage system comprises a waste gas absorption unit , an amine liquid circulation unit , a carbon dioxide gas salinization unit and a carbon sequestration unit which are communicated in sequence ; the system further comprises a limestone slurry pulping and filling unit ; and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit . The carbon capture and storage method is a brand - new organic amine decarburization and permanent carbon sequestration method provided on the basis of the principle of enhancing rock weathering ; compared with a traditional carbon sequestration method that carbon dioxide is transported through compression and liquefaction and stored in an underground salt water layer , the method has the advantages that the carbon capturing and storing process is short , high - pressure and low - temperature high - energy - consumption equipment does not need to be used , the captured carbon dioxide gas does not need to be stored and transported at low temperature , energy consumption can be reduced , the carbon sequestration cost is saved , and the carbon sequestration efficiency is improved . The carbon dioxide escape phenomenon in the storage and transportation process can be avoided , and the carbon sequestration efficiency is improved . \|Title\|(CN119607861 A)\|Carbon capture and storage system and carbon capture and storage method \|Advantages / Prev. Drawbacks\|(CN119607861 A)\|Compared with the prior art , the invention has the advantages that : ( 1 ) The invention provides a carbon capture storage system and a carbon capture storage method , wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle ; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine , then resolving the carbon dioxide gas in a desorption tower , then reacting ( . . . ) method of carbon dioxide through compression , liquefaction and transportation and underground salty water layer sealing , the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short , high - pressure and low - temperature high - energy equipment is not needed in the carbon capture and sealing process , the low - temperature storage and transportation of captured carbon dioxide gas are not needed , the energy consumption can be reduced , the carbon fixation cost can be saved , the phenomenon ( . . . ) meanwhile , the consumption in the aspects of manpower and material resources can be reduced , and the problems of overlong carbon capture and sealing flow , high energy consumption , high cost , high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved . \|Independent Claims\|(CN119607861 A)\|1. The carbon capturing and storing system is characterized by comprising an exhaust gas absorbing unit , an amine liquid circulating unit , a carbon dioxide gas salinization unit , a carbon fixation and sealing unit and a limestone slurry pulping and filling unit ; ( . . . ) \|	Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-053/96\|B01D-2258/0283\|C01B-032/55		B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-053/96\|B01D-2258/0283\|C01B-032/55	B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-053/96\|C01B-032/55	B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-053/96\|C01B-032/55			CN119838413	CN119838413 114246229 WHO=Examiner SELF=N CAT=A						PENDING	(CN119607861)\|PENDING	ALIVE	(CN119607861)\|ALIVE	(CN119607861)\|LEGAL DETAILS FOR CN119607861\|Actual or expected expiration date=2044-12-31\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-12-31\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202411977823\|Application date=2024-12-31\|Standardized application number=2024CN-1977823\|Event publication date=2025-03-14\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN119607861\|Publication stage code=A\|Publication date=2025-03-14\|Standardized publication number=CN119607861\|Event publication date=2025-03-14\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2025-04-01\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN119607861)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTcM0PYETPPhlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000076748113&ekey=2056&xpn=CN119607861&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=X3YLgN33UC9MvSpo4Kvsq5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN119607861)\|CN	(CN119607861)\|NAME=SINOTECH ENERGY CO., LTD. , COUNTRY=CN				(CN119607861)\|NAME=WEI YING\|NAME=HE WEI	(CN119607861)\|1	1	1					(CN119607861)\|Number of Claims: NCL=9\|Gazette date: GAZDATE=2025-03-14\|Gazette number: GAZNUM=41-1102\|Number of Pages: NPAGES=10\|		(CN119607861)\|CHINESE (CHI)	(CN119607861)\|Patent	Titre: (CN119607861)\|Carbon capture and storage system and carbon capture and storage method Résumé: (CN119607861)\|The invention relates to the technical field of flue gas treatment, in particular to a carbon capture and storage system and a carbon capture and storage method.The carbon capture and storage system comprises a waste gas absorption unit, an amine liquid circulation unit, a carbon dioxide gas salinization unit and a carbon sequestration unit which are communicated in sequence; the system further comprises a limestone slurry pulping and filling unit; and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. The carbon capture and storage method is a brand-new organic amine decarburization and permanent carbon sequestration method provided on the basis of the principle of enhancing rock weathering; compared with a traditional carbon sequestration method that carbon dioxide is transported through compression and liquefaction and stored in an underground salt water layer, the method has the advantages that the carbon capturing and storing process is short, high-pressure and low-temperature high-energy-consumption equipment does not need to be used, the captured carbon dioxide gas does not need to be stored and transported at low temperature, energy consumption can be reduced, the carbon sequestration cost is saved, and the carbon sequestration efficiency is improved. The carbon dioxide escape phenomenon in the storage and transportation process can be avoided, and the carbon sequestration efficiency is improved.	5	Abstract	gpt-4o-mini	no	The article focuses on a carbon capture and storage system related to flue gas treatment, which does not align with the topic of enhanced weathering and mineral carbonation.
7	AU2007900853\|AU2007902727\|AU2007906379\|AU2008217572\|WOAU2008/000232\|AU2009250983	WOAU2008/000232\|AU2009250983\|IN6026/DELNP/2009\|CA2678800\|KR10-2009-7019662\|CN200880006610\|JP2009550646\|US12/527,608\|EP08706115\|AU2008217572	IN293376\|CA2678800\|KR10-1527365\|CN101641145\|JP5345954\|US8496897\|EP2134449\|IN6026/DELNP/2009\|EP2134449\|JP2010519027\|AU2008217572\|CN101641145\|US20100021362\|AU2009250983\|EP2134449\|KR10-2009-0125109\|AU2008217572\|CA2678800\|WO2008/101293	6597398	WO2008/101293 A1 2008-08-28 [WO2008101293]\|AU2009250983 A1 2010-01-14 [AU2009250983]\|IN293376 B 2018-02-26 [IN-293376]\|IN6026/DELNP/2009 A 2011-08-26 [IN2009DN06026]\|CA2678800 C 2015-11-24 [CA2678800]\|CA2678800 A1 2008-08-28 [CA2678800]\|KR10-1527365 B1 2015-06-22 [KR101527365]\|KR10-2009-0125109 A 2009-12-03 [KR20090125109]\|CN101641145 B 2014-05-07 [CN101641145B]\|CN101641145 A 2010-02-03 [CN101641145]\|JP5345954 B2 2013-11-20 [JP5345954]\|JP2010519027 A 2010-06-03 [JP2010519027]\|US8496897 B2 2013-07-30 [US8496897]\|US20100021362 A1 2010-01-28 [US20100021362]\|EP2134449 B1 2012-10-10 [EP2134449]\|EP2134449 A4 2011-03-30 [EP2134449]\|EP2134449 A1 2009-12-23 [EP2134449]\|AU2008217572 B2 2010-02-04 [AU2008217572]\|AU2008217572 A1 2008-08-28 [AU2008217572]	2007-02-20\|2007-05-22\|2007-11-21\|2008-02-20\|2009-12-16	2008-02-20\|2009-12-16\|2009-09-18\|2008-02-20\|2008-02-20\|2008-02-20\|2008-02-20\|2008-02-20\|2008-02-20\|2008-02-20	2018-02-26\|2015-11-24\|2015-06-22\|2014-05-07\|2013-11-20\|2013-07-30\|2012-10-10\|2011-08-26\|2011-03-30\|2010-06-03\|2010-02-04\|2010-02-03\|2010-01-28\|2010-01-14\|2009-12-23\|2009-12-03\|2008-08-28\|2008-08-28\|2008-08-28	(EP2134449)\|2012-10-10\|(US8496897)\|2013-07-30\|\|(JP5345954)\|2013-11-20\|(CN101641145B)\|2014-05-07\|(IN-293376)\|2018-02-26\|(CA2678800)\|2015-11-24\|(KR101527365)\|2015-06-22\|(AU2008217572)\|2010-02-04\|	(EP2134449)\|2018-10-31\|(US8496897)\|2021-09-06\|(WO2008/101293)\|2010-08-20\|(JP5345954)\|2018-08-23\|(CN101641145)\|2018-02-20\|(IN293376)\|2028-02-20\|(CA2678800)\|2019-02-20\|(KR10-1527365)\|2018-06-04\|(AU2008217572)\|2018-09-13\|(AU2009250983)\|2010-12-02	(EP2134449)\|System, apparatus and method for carbon dioxide sequestration	(EP2134449)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.	HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD ([AU])\|RICHARD J HUNWICK\|HUNWICK, RICHARD J.\|HUNWICK RICHARD J.\|HUNWICK RICHARD J. ([AU])\|Richard Jay Han Wick\|HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD J ([AU])	(EP2134449)\|Hunwick, Richard J. ([AU])\|(EP2134449)\|Hunwick, Richard J. ([AU])\|(EP2134449)\|Hunwick, Richard J. ([AU])\|(US8496897)\|Hunwick Richard J ([AU])\|(US20100021362)\|HUNWICK RICHARD J\|(WO2008/101293)\|HUNWICK, Richard J. ([AU])\|(JP5345954)\|Richard Jay Han Wick\|(JP2010519027)\|Richard Jay Han Wick\|(CN101641145)\|HUNWICK RICHARD J. ([AU])\|(CN101641145)\|HUNWICK RICHARD J. ([AU])\|(IN293376)\|RICHARD J HUNWICK\|(IN6026/DELNP/2009)\|RICHARD J HUNWICK ([AU])\|(CA2678800)\|HUNWICK, RICHARD J. ([AU])\|(CA2678800)\|HUNWICK, RICHARD J. ([AU])\|(KR10-1527365)\|HUNWICK RICHARD J.\|(KR10-2009-0125109)\|HUNWICK RICHARD J.\|(AU2008217572)\|HUNWICK, RICHARD J.\|(AU2008217572)\|RICHARD HUNWICK\|(AU2009250983)\|HUNWICK, RICHARD	HUNWICK RICHARD J	(EP2134449)\|Hunwick, Richard J.\|(EP2134449)\|Hunwick, Richard J.\|(EP2134449)\|Hunwick, Richard J.	(EP2134449)\|Williams, Richard Andrew Norman;Harrison Goddard Foote ([GB])\|Reg. Nb: 100754772\|(US8496897)\|Frommer Lawrence & Haug LLP\|Santucci Ronald R\|(WO2008/101293)\|GRIFFITH HACK ([AU])\|(JP5345954)\|YOSHIDA Kenji\|Reg. Nb: 100075258\|ISHIDA Jun\|Reg. Nb: 100096976\|(CN101641145)\|CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11314\|(CA2678800)\|MBM INTELLECTUAL PROPERTY LAW LLP ([CA])\|(KR10-2009-0125109)\|HALLA PATENT & LAW FIRM	(EP2134449)\|A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor.\|It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations.\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\|Should it arise that the content of limestone or dolomite in the coal fuel is inadequate for the duty (as is likely to be the case with most power station fly ashes), it is possible to dose the appropriate quantity of pulverised limestone or dolomite to the power station boilers (not shown).\|The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s).\|	(EP2134449)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) in a third stage, passing the reactive slurry from (ii) through a reactor (52,70) that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|16. A system for (10) sequestering carbon dioxide from a gas stream, the system for comprising: (a) a first apparatus (28,30) for removing the carbon dioxide from the gas stream and for absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and (b) a reactor (52,70) for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|	(EP2134449)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|In accordance with a second aspect, the present invention provides a system for sequestering carbon dioxide from a gas stream, the system comprising: (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and (b) a reactor for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|	(EP2134449)\|METHANEDIONE(100,65)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,11)\|SEQUESTRATION(100,8)\|METHANEDIONE SEQUESTRATION(100,7)\|REACTION SLURRY(77,25)\|AMMONIATED SLURRY(70,6)\|METAL SILICATE(63,40)\|METAL SILICATE SLURRY(63,34)\|LIMESTONE PULVERIZATION(60,1)\|METHANEDIONE ISOLATION(56,1)\|REACTOR(50,25)\|METHANEDIONE CONVERSION(48,1)\|PERMANENT SEQUESTRATION(41,2)\|COAL FUEL(38,1)\|PRESSURIZED AMMONIA(36,1)\|AMMONIA(35,78)\|ABSORBED METHANEDIONE(34,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(34,1)\|METAL CARBONATE(32,12)\|NATURALLY OCCURRING SINK(30,1)\|PIPELINE(29,27)\|SCRUBBING CHAMBER(29,19)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|REACTION ENHANCEMENT(25,6)\|DOLOMITE(25,4)\|CHILLED SLURRY(25,3)\|SLURRY(23,41)\|AMMONIA ABSORPTION CHILLER(23,2)\|AMMONIA RECOVERY VESSEL(22,14)\|UNDERGROUND CHAMBER(22,10)\|EVAPORATION CHAMBER(21,1)\|REACTOR CONTROL(21,1)\|FLOW PATH(20,14)\|POWER STATION BOILER(20,1)\|MAGNESIUM SILICATE(18,2)\|AMMONIA WATER(17,18)\|METAL SILICATE ROCK(17,2)\|DUTY(15,2)\|OVERLAND AMMONIA PIPELINE(14,2)\|CARBON CAPTURE(13,1)\|METAL CARBONATE PRODUCT(12,4)\|CHILLED AMMONIA WATER(12,3)\|RESIDUAL AMMONIA SCRUBBER(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|RESULTANT AMMONIA WATER(12,1)\|FLY ASH(11,7)\|AMMONIA ABSORPTION CHAMBER(11,5)\|POWER STATION FLY ASH(11,4)\|CENT METHANEDIONE(11,2)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|POWER STATION(10,24)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|SERPENTINE MG3SI2O(9,1)\|FLUE GAS(8,33)\|AMMONIA LOSS(8,4)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE REGENERATION(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|CARBONATION REACTION(7,2)\|CO2 ABSORBER(7,2)\|EVAPORATOR VESSEL(7,2)\|METHANEDIONE CONTENT(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|OLIVINE(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|ABSORBER AQ(6,1)\|AMMONIA STRIPPING(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTIVE SLURRY HEATING(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,4)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|WOLLASTONITE(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENT NITROGEN(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|LIQUID PRESSURIZATION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|WT SLURRY(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|SOX(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|\|(EP2134449)\|METHANEDIONE(100,65)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,11)\|SEQUESTRATION(100,8)\|METHANEDIONE SEQUESTRATION(100,7)\|REACTION SLURRY(77,25)\|AMMONIATED SLURRY(70,6)\|METAL SILICATE(63,40)\|METAL SILICATE SLURRY(63,34)\|LIMESTONE PULVERIZATION(60,1)\|METHANEDIONE ISOLATION(56,1)\|REACTOR(50,25)\|METHANEDIONE CONVERSION(48,1)\|PERMANENT SEQUESTRATION(41,2)\|COAL FUEL(38,1)\|PRESSURIZED AMMONIA(36,1)\|AMMONIA(35,78)\|ABSORBED METHANEDIONE(34,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(34,1)\|METAL CARBONATE(32,12)\|NATURALLY OCCURRING SINK(30,1)\|PIPELINE(29,27)\|SCRUBBING CHAMBER(29,19)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|REACTION ENHANCEMENT(25,6)\|DOLOMITE(25,4)\|CHILLED SLURRY(25,3)\|SLURRY(23,41)\|AMMONIA ABSORPTION CHILLER(23,2)\|AMMONIA RECOVERY VESSEL(22,14)\|UNDERGROUND CHAMBER(22,10)\|EVAPORATION CHAMBER(21,1)\|REACTOR CONTROL(21,1)\|FLOW PATH(20,14)\|POWER STATION BOILER(20,1)\|MAGNESIUM SILICATE(18,2)\|AMMONIA WATER(17,18)\|METAL SILICATE ROCK(17,2)\|DUTY(15,2)\|OVERLAND AMMONIA PIPELINE(14,2)\|CARBON CAPTURE(13,1)\|METAL CARBONATE PRODUCT(12,4)\|CHILLED AMMONIA WATER(12,3)\|RESIDUAL AMMONIA SCRUBBER(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|RESULTANT AMMONIA WATER(12,1)\|FLY ASH(11,7)\|AMMONIA ABSORPTION CHAMBER(11,5)\|POWER STATION FLY ASH(11,4)\|CENT METHANEDIONE(11,2)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|POWER STATION(10,24)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|SERPENTINE MG3SI2O(9,1)\|FLUE GAS(8,33)\|AMMONIA LOSS(8,4)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE REGENERATION(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|CARBONATION REACTION(7,2)\|CO2 ABSORBER(7,2)\|EVAPORATOR VESSEL(7,2)\|METHANEDIONE CONTENT(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|OLIVINE(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|ABSORBER AQ(6,1)\|AMMONIA STRIPPING(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTIVE SLURRY HEATING(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,4)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|WOLLASTONITE(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENT NITROGEN(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|LIQUID PRESSURIZATION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|WT SLURRY(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|SOX(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|\|(EP2134449)\|METHANEDIONE(100,65)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,11)\|SEQUESTRATION(100,8)\|METHANEDIONE SEQUESTRATION(100,7)\|REACTION SLURRY(77,25)\|AMMONIATED SLURRY(70,6)\|METAL SILICATE(63,40)\|METAL SILICATE SLURRY(63,34)\|LIMESTONE PULVERIZATION(60,1)\|METHANEDIONE ISOLATION(56,1)\|REACTOR(50,25)\|METHANEDIONE CONVERSION(48,1)\|PERMANENT SEQUESTRATION(41,2)\|COAL FUEL(38,1)\|PRESSURIZED AMMONIA(36,1)\|AMMONIA(35,78)\|ABSORBED METHANEDIONE(34,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(34,1)\|METAL CARBONATE(32,12)\|NATURALLY OCCURRING SINK(30,1)\|PIPELINE(29,27)\|SCRUBBING CHAMBER(29,19)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|REACTION ENHANCEMENT(25,6)\|DOLOMITE(25,4)\|CHILLED SLURRY(25,3)\|SLURRY(23,41)\|AMMONIA ABSORPTION CHILLER(23,2)\|AMMONIA RECOVERY VESSEL(22,14)\|UNDERGROUND CHAMBER(22,10)\|EVAPORATION CHAMBER(21,1)\|REACTOR CONTROL(21,1)\|FLOW PATH(20,14)\|POWER STATION BOILER(20,1)\|MAGNESIUM SILICATE(18,2)\|AMMONIA WATER(17,18)\|METAL SILICATE ROCK(17,2)\|DUTY(15,2)\|OVERLAND AMMONIA PIPELINE(14,2)\|CARBON CAPTURE(13,1)\|METAL CARBONATE PRODUCT(12,4)\|CHILLED AMMONIA WATER(12,3)\|RESIDUAL AMMONIA SCRUBBER(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|RESULTANT AMMONIA WATER(12,1)\|FLY ASH(11,7)\|AMMONIA ABSORPTION CHAMBER(11,5)\|POWER STATION FLY ASH(11,4)\|CENT METHANEDIONE(11,2)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|POWER STATION(10,24)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|SERPENTINE MG3SI2O(9,1)\|FLUE GAS(8,33)\|AMMONIA LOSS(8,4)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE REGENERATION(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|CARBONATION REACTION(7,2)\|CO2 ABSORBER(7,2)\|EVAPORATOR VESSEL(7,2)\|METHANEDIONE CONTENT(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|OLIVINE(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|ABSORBER AQ(6,1)\|AMMONIA STRIPPING(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTIVE SLURRY HEATING(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,4)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|WOLLASTONITE(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENT NITROGEN(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|LIQUID PRESSURIZATION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|WT SLURRY(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|SOX(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|\|(US8496897)\|METHANEDIONE SEQUESTRATION(100,16)\|SEQUESTRATION(100,10)\|METHANEDIONE SEQUESTRATION(100,9)\|ABSORPTION(100,3)\|AMMONIA ABSORPTION(100,3)\|AMMONIA ABSORPTION(100,2)\|REACTION SLURRY(73,27)\|METAL SILICATE SLURRY(70,35)\|PRESSURIZED AMMONIA(68,2)\|LIMESTONE PULVERIZATION(61,1)\|METHANEDIONE(59,59)\|METHANEDIONE ISOLATION(56,1)\|METAL SILICATE ROCK(54,5)\|AMMONIA RECOVERY(53,8)\|METHANEDIONE CONVERSION(48,1)\|PERMANENT SEQUESTRATION(42,2)\|EVAPORATOR(41,8)\|METAL SILICATE(40,35)\|SCRUBBING CHAMBER(39,21)\|COAL FUEL(39,1)\|AMMONIA(34,79)\|RECOVERY VESSEL(31,18)\|NATURALLY OCCURRING SINK(31,1)\|REACTOR(29,23)\|GAS STREAM(28,10)\|CHILLED AMMONIA WATER(28,5)\|PIPELINE(27,28)\|SLURRY(26,43)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|DOLOMITE(25,4)\|PYROXENE RICH MINERAL(24,2)\|AMMONIA RECOVERY VESSEL(22,14)\|AMMONIA LOSS(22,4)\|MAGNESIUM RICH SILICATE(21,5)\|EVAPORATION CHAMBER(21,1)\|AMMONIA WATER(20,19)\|POWER STATION BOILER(20,1)\|REACTION ENHANCEMENT(19,5)\|METAL CARBONATE(17,10)\|UNDERGROUND CHAMBER(16,10)\|DUTY(16,2)\|REACTOR CONTROL(16,2)\|PCT AU(15,1)\|RESIDUAL AMMONIA SCRUBBER(14,4)\|OVERLAND AMMONIA PIPELINE(14,2)\|CARBON CAPTURE(13,1)\|FLY ASH(12,7)\|OLIVINE(12,5)\|AMMONIATED SLURRY(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|FLOW PATH(11,9)\|AMMONIA ABSORPTION CHAMBER(11,5)\|POWER STATION FLY ASH(11,4)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|PUBLICATION NUMBER(11,1)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE CAPTURE(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CO2 ABSORBER(9,3)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|FLUE GAS(8,33)\|POWER STATION(8,24)\|METAL CARBONATE PRODUCT(8,3)\|CHILLED SLURRY(8,2)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|METHANEDIONE CONTENT(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|PRETREATMENT HARD CRUSHING(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|EVAPORATOR VESSEL(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|AMMONIA STRIPPING(6,1)\|DENSER SLURRY(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PIPELINE VELOCITY(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|MAGNESIUM ION(5,2)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA ABSORPTION CHILLER(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|CORE CARBONATION REACTION(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SILICATE SLURRY DENSITY(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,5)\|MWE(4,5)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|MG3SI2O(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|LIQUID PRESSURIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|T WT SLURRY(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|SOX(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BEDROCK(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|\|(US20100021362)\|AMMONIA(100,84)\|METHANEDIONE(100,67)\|SLURRY(100,43)\|METAL SILICATE SLURRY(100,37)\|PIPELINE(100,30)\|REACTION SLURRY(100,27)\|AMMONIA WATER(100,20)\|METHANEDIONE SEQUESTRATION(100,16)\|FLOW PATH(100,14)\|GAS STREAM(100,12)\|SEQUESTRATION(100,10)\|METHANEDIONE SEQUESTRATION(100,9)\|CARBON SEQUESTRATION(100,8)\|ABSORPTION(100,4)\|METAL SILICATE ROCK(100,4)\|METAL SILICATE ROCK SLURRY(100,4)\|CARBON SEQUESTRATION(100,3)\|AMMONIA ABSORPTION(100,2)\|FLOW PATH PROVISION(100,1)\|LIMESTONE PULVERIZATION(61,1)\|METAL SILICATE(59,41)\|METHANEDIONE ISOLATION(56,1)\|AMMONIATED SLURRY(54,5)\|METHANEDIONE CONVERSION(48,1)\|MAGNESIUM RICH SILICATE(47,7)\|REACTOR(42,27)\|PERMANENT SEQUESTRATION(42,2)\|METAL CARBONATE(40,14)\|EVAPORATOR(39,8)\|COAL FUEL(39,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(35,1)\|SCRUBBING CHAMBER(34,20)\|NATURALLY OCCURRING SINK(31,1)\|REACTION ENHANCEMENT(30,6)\|LIQUID PRESSURIZATION(28,2)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|DOLOMITE(25,4)\|CHILLED SLURRY(25,3)\|AMMONIA ABSORPTION CHILLER(23,2)\|AMMONIA RECOVERY VESSEL(22,14)\|AMMONIA LOSS(22,4)\|AMMONIA ABSORPTION CHAMBER(21,6)\|CHAMBER PRESSURIZATION(21,1)\|EVAPORATION CHAMBER(21,1)\|POWER STATION BOILER(20,1)\|UNDERGROUND CHAMBER(16,10)\|DUTY(16,2)\|REACTOR CONTROL(16,2)\|RESIDUAL AMMONIA SCRUBBER(14,4)\|OVERLAND AMMONIA PIPELINE(14,2)\|RECIRCULATION(14,2)\|CARBON CAPTURE(13,1)\|FLY ASH(12,7)\|OLIVINE(12,5)\|METAL CARBONATE PRODUCT(12,4)\|CHILLED AMMONIA WATER(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|POWER STATION FLY ASH(11,4)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE CAPTURE(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CO2 ABSORBER(9,3)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|FLUE GAS(8,33)\|POWER STATION(8,24)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|METHANEDIONE CONTENT(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|EVAPORATOR VESSEL(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|AMMONIA STRIPPING(6,1)\|DENSER SLURRY(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PIPELINE VELOCITY(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|MAGNESIUM ION(5,2)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|CORE CARBONATION REACTION(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SILICATE SLURRY DENSITY(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,5)\|MWE(4,5)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|MG3SI2O(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|T WT SLURRY(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BEDROCK(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|FINAL CARBONATE PRODUCT SLURRY(3,1)\|\|(WO2008/101293)\|AMMONIA(100,75)\|METHANEDIONE(100,56)\|SLURRY(100,45)\|METAL SILICATE(100,39)\|METAL SILICATE SLURRY(100,31)\|PIPELINE(100,25)\|REACTION SLURRY(100,24)\|AMMONIA WATER(100,16)\|GAS STREAM(100,10)\|FLOW PATH(100,9)\|CARBON SEQUESTRATION(100,7)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|ABSORPTION(100,2)\|CARBON SEQUESTRATION(100,2)\|METAL SILICATE ROCK(100,2)\|METAL SILICATE ROCK SLURRY(100,2)\|AMMONIA ABSORPTION(100,1)\|FLOW PATH PROVISION(100,1)\|METHANEDIONE SEQUESTRATION(88,15)\|MAGNESIUM RICH SILICATE(74,9)\|AMMONIATED SLURRY(68,5)\|EVAPORATOR(55,6)\|METAL CARBONATE(54,11)\|REACTOR(47,22)\|LIQUID PRESSURIZATION(45,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(44,1)\|REACTION ENHANCEMENT(43,4)\|AMMONIA ABSORPTION CHAMBER(38,6)\|CHILLED SLURRY(32,3)\|AMMONIA ABSORPTION CHILLER(29,2)\|AMMONIA RECOVERY VESSEL(28,14)\|PYROXENE SILICATE METAL(27,2)\|OLIVINE(23,7)\|EVAPORATOR CHAMBER(23,6)\|UNDERGROUND CHAMBER(18,8)\|RESIDUAL AMMONIA SCRUBBER(18,4)\|OVERLAND AMMONIA PIPELINE(18,2)\|RECIRCULATION(18,2)\|METAL CARBONATE PRODUCT(15,4)\|CHILLED AMMONIA WATER(15,3)\|METHANEDIONE PERMANENT SEQUESTRATION(15,1)\|CENT METHANEDIONE(14,2)\|CHAMBER PRODUCT(14,2)\|ABSORBENT SLURRY DELUGING SPRAY(14,1)\|MINERAL CARBONATION(13,3)\|PRODUCING CHAMBER(13,2)\|RESIDUAL METHANEDIONE SCRUBBER(13,1)\|AMMONIA BUBBLE(12,3)\|CO2 ABSORBER(12,3)\|HUNTER VALLEY(12,2)\|METHANEDIONE SINK(12,2)\|TARGET METAL(12,2)\|FLUE GAS(11,33)\|POWER STATION(11,21)\|RETURN PIPELINE(11,5)\|INSOLUBLE CARBONATE(11,3)\|MOLL CO2(11,3)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|UNDERGROUND REACTOR(11,2)\|CARBONATED SILICATE SLURRY(11,1)\|METHANEDIONE TONNE(11,1)\|METHANEDIONE CONTENT(10,2)\|BLACK COAL MWE(10,1)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|FINAL EMPLACEMENT REHABILITATION(10,1)\|FIROM HOT SLURRY RISING(10,1)\|INCOMING REACTANT PIPELINE(10,1)\|METHANEDIONE SCRUBBING CHAMBER(10,1)\|SILICATE SLURRY CIRCULATION(10,1)\|RAW FLUE GAS(9,6)\|AMMONIA LOSS(9,3)\|CARBONATION REACTION(9,2)\|EVAPORATOR VESSEL(9,2)\|FIRED ELECTRICITY GENERATION PLANT(9,2)\|AMMONIA TONNE(9,1)\|BICARBONATE ISIH4HCO(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|FIN FAN COOLER(9,1)\|INCOMING SILICATE SLURRY(9,1)\|INSOLUBLE MAGNESIA(9,1)\|MAXIMIZE REGENERATION(9,1)\|METHANEDIONE ABSORPTION ZONE(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OVERLAND PIPELINE(9,1)\|REACTED SLURRY RISING(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(9,1)\|STACKED SUBCHAMBER(9,1)\|FLUE GAS FILTER(8,5)\|POWER STATION FLUE GAS(8,5)\|REACTION SOLUTION(8,5)\|CARBON DIOXIDE(8,3)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|SLURRY FEED(7,2)\|ABSORBER AQ(7,1)\|AMMONIA STRIPPING(7,1)\|EMPLACEMENT SITE(7,1)\|FIRED BOILER(7,1)\|HARMFUL METHANEDIONE GAS(7,1)\|LJUNGSTROM ROTARY(7,1)\|PERMANENT EMPLACEMENT(7,1)\|PRESSURIZED AMMONIA PASS(7,1)\|RAW REACTIVE SLURRY(7,1)\|REDUCING METHANEDIONE EMISSION(7,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(7,1)\|POWER STATION SITE(6,7)\|CONDENSATION(6,3)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA MILLION(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBONATE MINERAL(6,1)\|CONCENTRATED AMMONIA(6,1)\|CONCENTRIC PIPE(6,1)\|FINAL PERMANENT REPOSITORY(6,1)\|GAS REMNANT(6,1)\|GEHO PUMP(6,1)\|INORGANIC COMPONENT(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|NATURAL SILICATE(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRETREATMENT EXTENT(6,1)\|PYROXENE RICH MINERAL(6,1)\|RAW SLURRY(6,1)\|REACTED SLURRY RISE(6,1)\|RECOVERED AMMONIA(6,1)\|RESIDUAL VAPOR(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE CONVERSION(6,1)\|SLURRY REACTION(6,1)\|TRANSPORTING ORE(6,1)\|PRESSURE EXCHANGE(5,11)\|FINAL PRODUCT SLURRY(5,4)\|00O T(5,2)\|ADJACENT FLOW PATH(5,2)\|AGITATION(5,2)\|BOTTOM ASH PULVERIZATION(5,2)\|DOLOMITE(5,2)\|LIMESTONE(5,2)\|MG3SI2O(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AMMONIA SALT(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|HOT PRODUCT PIPELINE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|METHANEDIONE SOURCE(5,1)\|OXIDE REACTION(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|VAPORIZED AMMONIA FLOW(5,1)\|WT SLURRY(5,1)\|REACTION CHAMBER(4,4)\|METAL SILICATE SOLUTION(4,3)\|POWER STATION FLY ASH(4,3)\|SOX(4,3)\|STEAM(4,3)\|INSULATION(4,2)\|AIR PREHEATING(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CO2ZGWH(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|\|(JP5345954)\|METHANEDIONE(100,72)\|GAS STREAM(100,15)\|METHANEDIONE ISOLATION(100,12)\|ISOLATION(100,6)\|METHANEDIONE ISOLATION(100,6)\|METHANEDIONE REACTION(89,6)\|AMMONIATION SLURRY(78,2)\|METAL SILICATE SLURRY(71,38)\|REACTION SLURRY(65,27)\|SOCIAL CIRCUMSTANCE(64,1)\|METAL SILICATE(62,40)\|MAGNESIUM CONTENT SILICATE(52,3)\|SILICATE SLURRY(49,26)\|REACTOR(48,31)\|CONTRACTION METHANEDIONE(45,1)\|PIPELINE(43,38)\|COLD SLURRY(39,1)\|AMMONIA(37,71)\|DISPERSED METAL SILICATE(37,1)\|AMMONIA ABSORPTION RECOVERY CONTAINER(36,1)\|UNDERGROUND CHAMBER(33,4)\|AMMONISED SLURRY(33,2)\|METAL CARBONATE(31,11)\|SUBTERRANEAN INSTALLED CHAMBER(31,1)\|METHANEDIONE STREAM(30,2)\|PIPELINE SPEED(29,1)\|RECOVERY SLURRY REACTION(29,1)\|PRESSURIZED RECOVERY CONTAINER(28,2)\|NATURAL ABSORPTION(27,2)\|COLLECTION CONTAINER(27,1)\|METER(27,1)\|PRESSURIZED AMMONIA(25,3)\|SLURRY(23,35)\|AMMONIA ABSORPTION CHAMBER(23,7)\|FLOW PATH(22,10)\|AMMONIA LOSS(22,4)\|AMMONIA WATER(21,21)\|EVAPORATOR CHAMBER(20,7)\|COOLED SLURRY(19,4)\|METAL SILICATE ROCK SLURRY(19,2)\|FINAL FLUE GAS(19,1)\|REACTOR CONTROL(18,2)\|AMMONIA RECOVERY VESSEL(17,7)\|MINING STATION(16,9)\|FLOW CHANNEL(16,2)\|SLIP(16,1)\|RESIDUAL AMMONIA SCRUBBER(15,4)\|METHANEDIONE ISOLATING(15,3)\|REACTOR PRESSURE(15,1)\|CORUNDUITE(14,4)\|RECYCLING(14,2)\|FLUE GAS(13,35)\|LATE PARAGRAPH(13,4)\|METAL CARBONATE PRODUCT(13,4)\|AMMONIA BUBBLE(11,3)\|MINERAL CARBONATION(11,3)\|ABSORBED METHANEDIONE TON(11,1)\|INSOLUBLE MAGNESIA PRECIPITATION(11,1)\|RESIDUAL METHANEDIONE SCRUBBER(11,1)\|HEAT EXCHANGER(10,26)\|RETURN PIPELINE(10,5)\|CO2 ABSORBER(10,3)\|PULVERIZED COAL BURNING(10,1)\|POWER PLANT(9,31)\|COOLED AMMONIA WATER(9,4)\|HOT SILICATE SLURRY(9,2)\|HUNTER VALLEY(9,2)\|INCOMING REACTIVE SLURRY(9,2)\|UNDERGROUND REACTOR(9,2)\|INCOMING REACTANT PIPELINE(9,1)\|METHANEDIONE ABSORBER(9,1)\|METHANEDIONE SCRUBBING CHAMBER(9,1)\|SCRUBBING CHAMBER HEADSPACE(9,1)\|SERPENTINE MINING SITE(9,1)\|SILICATE SLURRY CIRCULATION(9,1)\|SPRAYED ABSORBENT SLURRY(9,1)\|STACKED SUBCHAMBER(9,1)\|REACTION SOLUTION(7,5)\|UNTREATED FLUE GAS(7,5)\|POWER PLANT FLUE GAS(7,4)\|EVAPORATOR CONTAINER(7,2)\|AMMONIATED SLURRY(7,1)\|CRUSHED LIMESTONE(7,1)\|FEEDSTOCK COAL(7,1)\|INCOMING SILICATE SLURRY(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|METHANEDIONE EMISSION(7,1)\|METHANEDIONE PROMOTING REACTION(7,1)\|MINING SITE VICINITY(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|SILICATE SLURRY COOLING(7,1)\|SUBTERRANEAN CHAMBER REACTOR(7,1)\|SUBTERRANEAN PIPELINE(7,1)\|SUPERBITTER ROCK(7,1)\|UNTREATED REACTIVE SLURRY(7,1)\|HEAT TRANSFER(6,2)\|HOT SLURRY(6,2)\|MAGNESIUM ION(6,2)\|PUMPING ENERGY(6,2)\|SLURRY FEED(6,2)\|AMMONIA COLLECTION VESSEL(6,1)\|AMMONIA VAPORIZATION(6,1)\|BURNING BOILER(6,1)\|CARBON ISOLATION NONLIMITING(6,1)\|COLD SILICATE SLURRY(6,1)\|COOLED SILICATE SLURRY(6,1)\|DEINKED ASH(6,1)\|DOLOMITE LIME(6,1)\|ECONOMIC STANDPOINT(6,1)\|FAN CONCENTRIC PIPE(6,1)\|GROUND AMMONIA PIPELINE(6,1)\|LJUNGSTROM ROTARY(6,1)\|METHANEDIONE CONVERSION(6,1)\|METHANEDIONE DISCHARGE(6,1)\|METHANEDIONE SEPARATION(6,1)\|MILLED SLURRY(6,1)\|RESIDUAL AMMONIA COLLECTOR(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|STEAM INJECTION(6,1)\|UNTREATED SLURRY(6,1)\|FINAL PRODUCT SLURRY(5,5)\|FLUE GAS FILTER(5,3)\|MG3SI2O(5,3)\|METHANEDIONE SOURCE(5,2)\|ALKALINE INDUSTRIAL RESIDUE(5,1)\|AMMONIA CONDENSATION(5,1)\|AMMONIA RECOVERY CONTAINER CONTENT(5,1)\|AMMONIA SLURRY(5,1)\|AMMONIA TON(5,1)\|BURNED ASH(5,1)\|BYPRODUCT SILICA(5,1)\|CARBONATE MINERAL(5,1)\|CIRCULATION NATURAL VELOCITY(5,1)\|CO2 MCO(5,1)\|COAL FUEL(5,1)\|COLLECTED AMMONIA(5,1)\|DISSOLVE TARGET(5,1)\|ELEMENTAL IRON(5,1)\|EVAPORATOR VESSEL(5,1)\|EXTRACT MAGNESIUM(5,1)\|INSOLUBLE CARBONATE SALT(5,1)\|MAGNESIA REACTION(5,1)\|METHANEDIONE CONTENT(5,1)\|MINE CAVITY(5,1)\|NATURAL DRAFT COOLING TOWER(5,1)\|NATURALLY OCCURRING SILICATE ROCK(5,1)\|PERMANENT INSULATION(5,1)\|PLANT FACILITY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTION SLURRY RISING(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|POWER PLANT FLY ASH(4,4)\|ANTIOFFICE(4,2)\|CARBAMATE(4,2)\|FINAL PLACEMENT LOCATION(4,2)\|MG2SIO(4,2)\|PARTICULATE(4,2)\|RAW FLUE GAS(4,2)\|SOUTH WALL(4,2)\|WOLLASTONITE(4,2)\|ABSORBING CHAMBER(4,1)\|ACTIVE SUBSTANCE OXIDATION(4,1)\|AMMONIA REACTION(4,1)\|AMMONIA REGENERATION RATE(4,1)\|AUDIT(4,1)\|BASELOAD MODE(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENTRAL CARBONATION REACTION(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|CONVEYANCE(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DESIRABLE SILICATE ROCK(4,1)\|DESIRED HEAT TRANSFER(4,1)\|DIFFUSED METAL SILICATE(4,1)\|DISCHARGE RECTIFICATION VESSEL(4,1)\|FIBROUS FILTER(4,1)\|FIN FAN(4,1)\|FRICTION LOSS(4,1)\|GEHO PUMP(4,1)\|HARMFUL METHANEDIONE GAS SOURCE(4,1)\|HYDROSTATIC HEAD USABLE DEPTH(4,1)\|LUMPY PRODUCT(4,1)\|MAGNESIUM RICH SILICATE(4,1)\|MAGNESIUM STABILITY(4,1)\|METHANEDIONE SEQUESTRATION(4,1)\|MILLED METAL SILICATE(4,1)\|NATURAL SILICATE(4,1)\|PERMANENT PLACEMENT(4,1)\|PIPE REACTOR(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PROMOTION(4,1)\|RADIITE SILICATE METAL(4,1)\|REACTION STEP(4,1)\|REINCREASE(4,1)\|RESIDUAL VAPOR(4,1)\|SLURRY SUPPLY(4,1)\|TRANSPORT FEW HOUR(4,1)\|TUBULAR REACTOR(4,1)\|AMBIENT TEMPERATURE(3,3)\|EXOTHERMIC REACTION(3,3)\|GWH(3,3)\|METAL SILICATE SOLUTION(3,3)\|MWE(3,3)\|ORE(3,3)\|ABSORB REMAINING MANIFEST HEAT(3,1)\|AIR PREHEATING(3,1)\|ALKALINITY(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA CONTENT(3,1)\|AMMONIA RECOVERY VESSEL TOP(3,1)\|AMMONIA REMOVAL(3,1)\|AMMONIA RICH SOLUTION(3,1)\|ANNULUS(3,1)\|BICARBONATE(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CLEAN FLUE GAS(3,1)\|COOL FILTER(3,1)\|COOLED FILTER FLUE GAS(3,1)\|\|(JP2010519027)\|AMMONIA(100,76)\|METHANEDIONE(100,71)\|METAL SILICATE(100,45)\|SLURRY(100,42)\|METAL SILICATE SLURRY(100,39)\|REACTION SLURRY(100,31)\|AMMONIA WATER(100,22)\|METHANEDIONE ISOLATION(100,14)\|GAS STREAM(100,13)\|FLOW PATH(100,8)\|ISOLATION(100,6)\|METHANEDIONE ISOLATION(100,6)\|ABSORPTION(100,4)\|METAL SILICATE ROCK(100,4)\|METAL SILICATE ROCK SLURRY(100,4)\|CARBON ISOLATION(100,3)\|AMMONIA ABSORPTION(100,2)\|METHANEDIONE REACTION(97,6)\|AMMONIATION SLURRY(71,1)\|SOCIAL CIRCUMSTANCE(65,1)\|ABSORBED METHANEDIONE(53,2)\|METAL CARBONATE(52,15)\|SILICATE SLURRY(50,27)\|REACTOR(49,30)\|SUBTERRANEAN FORMATION(46,1)\|PRESSURIZED AMMONIA(45,2)\|EVAPORATOR(44,8)\|COLD SLURRY(40,1)\|DISSOLVE TARGET(39,2)\|GAS TURBINE SUBTERRANEAN FORMATION(39,1)\|PIPELINE(37,35)\|DISPERSED METAL SILICATE(37,1)\|AMMONIA ABSORPTION RECOVERY CONTAINER(36,1)\|AMMONISED SLURRY(34,2)\|AMMONIA ABSORPTION CHAMBER(33,8)\|AMMONIA ABSORPTION CHILLER(31,1)\|CHAMBER INSTALLED UNDERGROUND(31,1)\|METHANEDIONE STREAM(30,2)\|PRESSURIZED RECOVERY CONTAINER(29,2)\|PIPELINE SPEED(29,1)\|NATURAL ABSORPTION(28,2)\|COLLECTION CONTAINER(27,1)\|METER(27,1)\|AMMONIA LOSS(23,4)\|CORUNDUITE(22,5)\|RADIITE SILICATE METAL(22,2)\|EVAPORATOR CHAMBER(20,7)\|COOLED SLURRY(19,4)\|FINAL FLUE GAS(19,1)\|AMMONIA RECOVERY VESSEL(18,7)\|REACTOR CONTROL(18,2)\|GAS TURBINE(18,1)\|MINING STATION(17,9)\|FLOW CHANNEL(17,2)\|SLIP(17,1)\|HEAT EXCHANGER(16,28)\|RESIDUAL AMMONIA SCRUBBER(16,4)\|TARGET METAL(16,4)\|REACTOR PRESSURE(16,1)\|METHANEDIONE ISOLATING(15,3)\|FLUE GAS(14,36)\|RECYCLING(14,2)\|LATE PARAGRAPH(13,4)\|METAL CARBONATE PRODUCT(13,4)\|POWER PLANT(12,33)\|HIGH MAGNESIUM CONTENT SILICATE(12,10)\|PRODUCING CHAMBER(12,2)\|AMMONIA BUBBLE(11,3)\|MINERAL CARBONATION(11,3)\|AMMONIATED SLURRY(11,2)\|ABSORBED METHANEDIONE TON(11,1)\|INSOLUBLE MAGNESIA PRECIPITATION(11,1)\|RESIDUAL METHANEDIONE SCRUBBER(11,1)\|RETURN PIPELINE(10,5)\|CO2 ABSORBER(10,3)\|PULVERIZED COAL BURNING(10,1)\|COOLED AMMONIA WATER(9,4)\|HOT SILICATE SLURRY(9,2)\|HUNTER VALLEY(9,2)\|INCOMING REACTIVE SLURRY(9,2)\|UNDERGROUND REACTOR(9,2)\|INCOMING REACTANT PIPELINE(9,1)\|METHANEDIONE ABSORBER(9,1)\|METHANEDIONE SCRUBBING CHAMBER(9,1)\|SCRUBBING CHAMBER HEADSPACE(9,1)\|SERPENTINE MINING SITE(9,1)\|SILICATE SLURRY CIRCULATION(9,1)\|SPRAYED ABSORBENT SLURRY(9,1)\|STACKED SUBCHAMBER(9,1)\|POWER PLANT FLUE GAS(8,4)\|EVAPORATOR CONTAINER(8,2)\|AMMONIA ABSORPTION COOLER(8,1)\|CRUSHED LIMESTONE(8,1)\|FEEDSTOCK COAL(8,1)\|INCOMING SILICATE SLURRY(8,1)\|METHANEDIONE ABSORPTION ZONE(8,1)\|METHANEDIONE EMISSION(8,1)\|MINING SITE VICINITY(8,1)\|MULTISTAGE BARREL PUMP(8,1)\|RESIDUAL AMMONIA ABSORBER(8,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(8,1)\|SILICATE SLURRY COOLING(8,1)\|SUBTERRANEAN CHAMBER REACTOR(8,1)\|SUBTERRANEAN PIPELINE(8,1)\|SUPERBITTER ROCK(8,1)\|UNTREATED REACTIVE SLURRY(8,1)\|REACTION SOLUTION(7,5)\|UNTREATED FLUE GAS(7,5)\|UNDERGROUND CHAMBER(7,2)\|HEAT TRANSFER(6,2)\|HOT SLURRY(6,2)\|MAGNESIUM ION(6,2)\|PUMPING ENERGY(6,2)\|SLURRY FEED(6,2)\|AMMONIA COLLECTION VESSEL(6,1)\|AMMONIA VAPORIZATION(6,1)\|BURNING BOILER(6,1)\|CARBON ISOLATION NONLIMITING(6,1)\|COLD SILICATE SLURRY(6,1)\|COOLED SILICATE SLURRY(6,1)\|DEINKED ASH(6,1)\|DOLOMITE LIME(6,1)\|ECONOMIC STANDPOINT(6,1)\|GROUND AMMONIA PIPELINE(6,1)\|LJUNGSTROM ROTARY(6,1)\|METHANEDIONE CONVERSION(6,1)\|METHANEDIONE DISCHARGE(6,1)\|METHANEDIONE SEPARATION(6,1)\|MILLED SLURRY(6,1)\|RESIDUAL AMMONIA COLLECTOR(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|STEAM INJECTION(6,1)\|UNTREATED SLURRY(6,1)\|FINAL PRODUCT SLURRY(5,5)\|FLUE GAS FILTER(5,3)\|MG3SI2O(5,3)\|CHAMBER PRODUCT FLOW PATH(5,2)\|METHANEDIONE SOURCE(5,2)\|ALKALINE INDUSTRIAL RESIDUE(5,1)\|AMMONIA CONDENSATION(5,1)\|AMMONIA RECOVERY CONTAINER CONTENT(5,1)\|AMMONIA TON(5,1)\|BURNED ASH(5,1)\|BYPRODUCT SILICA(5,1)\|CARBONATE MINERAL(5,1)\|CIRCULATION NATURAL VELOCITY(5,1)\|CO2 MCO(5,1)\|COAL FUEL(5,1)\|COLLECTED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|ELEMENTAL IRON(5,1)\|EVAPORATOR VESSEL(5,1)\|EXTRACT MAGNESIUM(5,1)\|INSOLUBLE CARBONATE SALT(5,1)\|MAGNESIA REACTION(5,1)\|METHANEDIONE CONTENT(5,1)\|MINE CAVITY(5,1)\|NATURAL DRAFT COOLING TOWER(5,1)\|NATURALLY OCCURRING SILICATE ROCK(5,1)\|PERMANENT INSULATION(5,1)\|PLANT FACILITY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTION SLURRY RISING(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|POWER PLANT FLY ASH(4,4)\|REACTION CHAMBER(4,4)\|CARBAMATE(4,2)\|FINAL PLACEMENT LOCATION(4,2)\|MG2SIO(4,2)\|PARTICULATE(4,2)\|RAW FLUE GAS(4,2)\|SOUTH WALL(4,2)\|WOLLASTONITE(4,2)\|ABSORBING CHAMBER(4,1)\|ACTIVE SUBSTANCE OXIDATION(4,1)\|AMMONIA REACTION(4,1)\|AMMONIA REGENERATION RATE(4,1)\|AUDIT(4,1)\|BASELOAD MODE(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENTRAL CARBONATION REACTION(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|CONVEYANCE(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DESIRABLE SILICATE ROCK(4,1)\|DESIRED HEAT TRANSFER(4,1)\|DISCHARGE RECTIFICATION VESSEL(4,1)\|FIBROUS FILTER(4,1)\|FIN FAN(4,1)\|FRICTION LOSS(4,1)\|GEHO PUMP(4,1)\|HARMFUL METHANEDIONE GAS SOURCE(4,1)\|HYDROSTATIC HEAD USABLE DEPTH(4,1)\|LUMPY PRODUCT(4,1)\|MAGNESIUM RICH SILICATE(4,1)\|MAGNESIUM STABILITY(4,1)\|METHANEDIONE SEQUESTRATION(4,1)\|MILLED METAL SILICATE(4,1)\|NATURAL SILICATE(4,1)\|PERMANENT PLACEMENT(4,1)\|PIPE REACTOR(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|REACTION STEP(4,1)\|REINCREASE(4,1)\|RESIDUAL VAPOR(4,1)\|SLURRY SUPPLY(4,1)\|TRANSPORT FEW HOUR(4,1)\|TUBULAR REACTOR(4,1)\|AMBIENT TEMPERATURE(3,3)\|EXOTHERMIC REACTION(3,3)\|GWH(3,3)\|METAL SILICATE SOLUTION(3,3)\|MWE(3,3)\|ORE(3,3)\|ABSORB REMAINING MANIFEST HEAT(3,1)\|AIR PREHEATING(3,1)\|ALKALINITY(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA CONTENT(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA RECOVERY VESSEL TOP(3,1)\|AMMONIA REMOVAL(3,1)\|AMMONIA RICH SOLUTION(3,1)\|ANNULUS(3,1)\|BICARBONATE(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CLEAN FLUE GAS(3,1)\|COOL FILTER(3,1)\|\|(CN101641145)\|CARBON DIOXIDE(100,114)\|SLURRY(100,42)\|REACTION SLURRY(100,32)\|CARBON DIOXIDE SEQUESTRATION(100,18)\|GAS STREAM(100,7)\|SEQUESTERING CARBON DIOXIDE(100,3)\|METAL SILICATE SLURRY(88,36)\|AMMONIA ABSORPTION RECOVERY VESSEL(79,1)\|METAL SILICATE(72,39)\|AMMONIATED SLURRY(71,5)\|CHAMBER REACTOR(71,3)\|ABSORPTION RECOVERY VESSEL(68,1)\|SUBTERRANEAN REACTOR(66,1)\|MAGNESIUM RICH SILICATE(54,7)\|REACTION SLURRY RISING(51,1)\|METAL CARBONATE(49,14)\|PERMANENT INSULATION(49,1)\|AMMONIA(48,63)\|METAL SILICATE ROCK(45,4)\|NATURALLY OCCURRING SINK(40,1)\|REACTOR(39,21)\|PHOTOSYNTHESIS(36,1)\|CHILLED SLURRY(35,2)\|PIPELINE REACTOR(33,4)\|CARBONATE PRODUCT(32,4)\|AMMONIA GAS BUBBLE(32,1)\|AMMONIA RECOVERY VESSEL(30,14)\|AMMONIA ABSORPTION CHILLER(30,2)\|AMMONIA LOSS(29,3)\|BIOMASS(28,1)\|EVAPORATION CHAMBER(28,1)\|SEPARATING CARBON DIOXIDE(27,1)\|CHAMBER PRODUCT(26,2)\|AMMONIA WATER(25,20)\|ELECTRICITY DEMAND(25,1)\|RAW FLUE GAS(21,6)\|METAL CARBONATE PRODUCT(21,4)\|REMOVING CARBON DIOXIDE(21,2)\|HEAT EXCHANGER(20,25)\|CARBON CAPTURE(20,1)\|RESIDUAL AMMONIA SCRUBBER(19,4)\|REACTION ENHANCEMENT(19,2)\|COLLECTION POINT(19,1)\|CHILLED AMMONIA WATER(17,2)\|PRESSURIZED LIQUID AMMONIA(17,2)\|BULK DENSITY(17,1)\|AMMONIA GAS(16,1)\|JACKETED ABOVEGROUND PIPELINE(16,1)\|FLUE GAS(15,33)\|AMMONIA ABSORPTION CHAMBER(15,5)\|MINERAL CARBONATION(14,3)\|ABSORBENT SLURRY DELUGE SPRAY(14,1)\|CARBON DIOXIDE COLLECTION POINT(14,1)\|SOUTH HUNTER VALLEY(14,1)\|POWER PLANT(13,31)\|INSOLUBLE CARBONATE(13,4)\|PRODUCING CHAMBER(13,3)\|AMMONIA ABSORPTION(13,2)\|CARBON DIOXIDE REACTION(13,2)\|ONSHORE AMMONIA PIPELINE(13,1)\|EVAPORATOR CHAMBER(12,5)\|WASHING CHAMBER(12,5)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|STATIC HEAD(10,3)\|AMMONIA BUBBLE(10,2)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|PRETREATMENT ABOVETHE EXTENT(10,1)\|RECYCLED SILICATE SLURRY(10,1)\|SCRUBBING CHAMBER HEADSPACE(10,1)\|STACKED SUBCOMPARTMENT(10,1)\|POWER PLANT FLUE GAS(9,5)\|REACTION SOLUTION(9,5)\|EVAPORATOR VESSEL(9,2)\|RECOVERING AMMONIA(9,2)\|CARBON DIOXIDEON CAPTURE(9,1)\|INCOMING SILICATE SLURRY(9,1)\|LOW NOX BURNER(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OLIVINE STONE(9,1)\|ONSHORE PIPELINE(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|AMMONIUM SALT(8,4)\|DOLOMITE(8,4)\|FLUE GAS FILTER(8,4)\|GAS MIXTURE(8,2)\|COLD SILICATE SLURRY(8,1)\|CRUDE REACTION SLURRY(8,1)\|DEINKING ASH(8,1)\|DELUGING SPRAY(8,1)\|DENSER SLURRY(8,1)\|LJUNGSTROM ROTARY(8,1)\|MAXIMIZE REGENERATION(8,1)\|OLIVINE RICH(8,1)\|POWDERED LIMESTONE(8,1)\|RECYCLED SCRUBBING MEDIUM(8,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(8,1)\|SERPENTINE STONE(8,1)\|SLURRY CIRCULATION(8,1)\|ULTIMATE LOCATION REHABILITATION(8,1)\|UNDERGROUND REACTOR(8,1)\|CARBON DIOXIDE TON(7,3)\|CARBON SEQUESTRATION(7,3)\|PUMPING ENERGY(7,2)\|POWER PLANT SITE(6,6)\|CONDENSATION(6,3)\|ALKALI INDUSTRY RESIDUE(6,1)\|AMMONIA FLASH(6,1)\|AMMONIA MILLION(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(6,1)\|CARBONATE MINERAL(6,1)\|COAL DUST BOILER(6,1)\|COAL FUEL(6,1)\|CONCENTRATED AMMONIA(6,1)\|CORE CARBONATION REACTION(6,1)\|DISSOLVE TARGET(6,1)\|FIN FAN COOLER(6,1)\|FROZEN METAL SILICATE SLURRY(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INSOLUBLE MAGNESIUM HYDROXIDE PRECIPITATION(6,1)\|MAGNESIUM PRECIPITATE(6,1)\|MINE VOID(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PUMPING CAPABILITY(6,1)\|PYROXENE RICH MINERAL(6,1)\|PYROXENE SILICATE METAL(6,1)\|RAW COAL(6,1)\|RAW SLURRY(6,1)\|REACTOR CHOICE(6,1)\|RESIDUAL STEAM(6,1)\|SCRUBBING MEDIA(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE SLURRY DENSITY(6,1)\|SILICATE SLURRY FLOW CARBONATION(6,1)\|TRANSPORTING ORE(6,1)\|CARBON DIOXIDE SEQUESTRATION(5,4)\|FINAL PRODUCT SLURRY(5,4)\|MAGNESIUM CARBONATE(5,4)\|POWER PLANT FLY ASH(5,4)\|PRESSURE EXCHANGE(5,4)\|ABSORBER DETAIL(5,2)\|ADJACENT FLOW PATH(5,2)\|CARBON DIOXIDE EMISSION(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AMMONIA RICH SOLUTION(5,1)\|AMMONIA TON HOUR(5,1)\|CARBONATE SILICATE SLURRY(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|CONCENTRIC TUBE(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|FINAL COLD SLURRY FEED(5,1)\|FLASH RECTIFIER VESSEL(5,1)\|FRICTION LOSS(5,1)\|GRADUAL DECREASE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|MILLION KILOWATT HOUR(5,1)\|NATURAL DRAFT COOLING TOWER(5,1)\|PARTICLE CLEANING(5,1)\|PERMANENT PLACEMENT(5,1)\|PREPROCESSING(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|REJUVENATION(5,1)\|SLURRY COOLING(5,1)\|STEAM TON HOUR(5,1)\|STRATEGIC LOCATION(5,1)\|SUPPLEMENTAL HEATING(5,1)\|TUBE BUNDLE(5,1)\|WET GRINDING(5,1)\|JET PUMP(4,4)\|AMBIENT TEMPERATURE(4,3)\|BLACK COAL(4,3)\|EXOTHERMIC REACTION(4,3)\|HYDROSTATIC HEAD(4,3)\|SHELL(4,2)\|SINGLE INTEGRATED(4,2)\|ABSORB REMAINING SENSIBLE HEAT(4,1)\|AIR PREHEATING(4,1)\|ALKALI RICH METAL SILICATE(4,1)\|AMMONIA ABSORBER(4,1)\|AMMONIA CONTENT(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA RECOVERY VESSEL BOTTOM(4,1)\|AMMONIA RECOVERY VESSEL TOP(4,1)\|AMMONIASHOULD(4,1)\|AMMONIUM CARBONATE COMPOUND(4,1)\|ARRIVAL PRESSURE(4,1)\|BASEMENT DESIGN(4,1)\|BEDROCK(4,1)\|BICARBONATE(4,1)\|BOTTOM ASH PULVERIZATION(4,1)\|BULK PRODUCT(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CARBON DIOXIDE ABSORPTION ZONE(4,1)\|CARBON DIOXIDE SCRUBBER CHAMBER(4,1)\|CARBON DIOXIDE SCRUBBING MEDIUM(4,1)\|CARBON DIOXIDE SINK(4,1)\|CHILLED SOLUTION(4,1)\|CLEAN FLUE GAS(4,1)\|COAGULATION(4,1)\|COMMINUTION(4,1)\|CONDUCTING CARBON DIOXIDE(4,1)\|CONSTRUCTED STORAGE COMPARTMENT(4,1)\|COOLER GAS(4,1)\|DESTRUCTION(4,1)\|DOSING(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|ENERGY BURDEN(4,1)\|EXCESS HEAT(4,1)\|\|(CN101641145)\|CARBON DIOXIDE(100,117)\|AMMONIA(100,66)\|METAL SILICATE(100,45)\|SLURRY(100,43)\|METAL SILICATE SLURRY(100,36)\|REACTION SLURRY(100,32)\|AMMONIA WATER(100,20)\|CARBON DIOXIDE SEQUESTRATION(100,18)\|PIPELINE(100,15)\|FLOW PATH(100,11)\|CARBON SEQUESTRATION(100,9)\|GAS STREAM(100,7)\|ABSORPTION(100,5)\|CARBON DIOXIDE SEQUESTRATION(100,5)\|SEQUESTRATION(100,5)\|METAL SILICATE ROCK(100,4)\|METAL SILICATE ROCK SLURRY(100,4)\|CARBON SEQUESTRATION(100,3)\|SEQUESTERING CARBON DIOXIDE(100,3)\|AMMONIA ABSORPTION(100,2)\|MAGNESIUM RICH SILICATE(77,9)\|AMMONIATED SLURRY(68,5)\|SUBTERRANEAN REACTOR(63,1)\|METAL CARBONATE(54,15)\|REACTOR(53,26)\|EVAPORATOR(52,8)\|REACTION SLURRY RISING(49,1)\|PERMANENT INSULATION(46,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(43,1)\|NATURALLY OCCURRING SINK(38,1)\|AMMONIA ABSORPTION CHAMBER(37,7)\|FROZEN SLURRY(37,1)\|PHOTOSYNTHESIS(34,1)\|AMMONIA GAS BUBBLE(31,1)\|LIQUID PRESSURIZATION(30,2)\|AMMONIA RECOVERY VESSEL(29,14)\|AMMONIA ABSORPTION CHILLER(29,2)\|AMMONIUM SALT(27,5)\|AMMONIA LOSS(27,3)\|PYROXENE SILICATE METAL(27,2)\|BIOMASS(27,1)\|SEPARATING CARBON DIOXIDE(25,1)\|ELECTRICITY DEMAND(24,1)\|EVAPORATOR CHAMBER(23,6)\|CARBON DIOXIDE REACTION(21,2)\|RAW FLUE GAS(20,6)\|REMOVING CARBON DIOXIDE(20,2)\|CARBON CAPTURE(19,1)\|RESIDUAL AMMONIA SCRUBBER(18,4)\|TARGET METAL(18,4)\|REACTION ENHANCEMENT(18,2)\|COLLECTION POINT(18,1)\|FLUE GAS(16,34)\|CHILLED AMMONIA WATER(16,2)\|BULK DENSITY(16,1)\|POWER PLANT(15,33)\|METAL CARBONATE PRODUCT(15,4)\|AMMONIA GAS(15,1)\|JACKETED ABOVEGROUND PIPELINE(15,1)\|CHAMBER PRODUCT(14,2)\|ABSORBENT SLURRY DELUGE SPRAY(14,1)\|CARBON DIOXIDE COLLECTION POINT(14,1)\|SOUTH HUNTER VALLEY(14,1)\|MINERAL CARBONATION(13,3)\|PIPELINE REACTOR(13,3)\|INSOLUBLE CARBONATE(12,4)\|PRODUCING CHAMBER(12,3)\|ONSHORE AMMONIA PIPELINE(12,1)\|WASHING CHAMBER(11,5)\|AMMONIA BUBBLE(10,2)\|HOT SILICATE SLURRY(10,2)\|INCOMING REACTIVE SLURRY(10,2)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|RECYCLED SILICATE SLURRY(10,1)\|SCRUBBING CHAMBER HEADSPACE(10,1)\|STACKED SUBCOMPARTMENT(10,1)\|STATIC HEAD(9,3)\|EVAPORATOR VESSEL(9,2)\|RECOVERING AMMONIA(9,2)\|INCOMING SILICATE SLURRY(9,1)\|LOW NOX BURNER(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OLIVINE STONE(9,1)\|ONSHORE PIPELINE(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|POWER PLANT FLUE GAS(8,5)\|REACTION SOLUTION(8,5)\|GAS MIXTURE(8,2)\|DOLOMITE(7,4)\|FLUE GAS FILTER(7,4)\|PUMPING ENERGY(7,2)\|CHILLED SLURRY(7,1)\|COLD SILICATE SLURRY(7,1)\|CRUDE REACTION SLURRY(7,1)\|DEINKING ASH(7,1)\|DELUGING SPRAY(7,1)\|DENSER SLURRY(7,1)\|LJUNGSTROM ROTARY(7,1)\|MAXIMIZE REGENERATION(7,1)\|OLIVINE RICH(7,1)\|POWDERED LIMESTONE(7,1)\|RECYCLED SCRUBBING MEDIUM(7,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(7,1)\|SERPENTINE STONE(7,1)\|SLURRY CIRCULATION(7,1)\|ULTIMATE LOCATION REHABILITATION(7,1)\|UNDERGROUND REACTOR(7,1)\|POWER PLANT SITE(6,6)\|CARBON DIOXIDE TON(6,3)\|ALKALI INDUSTRY RESIDUE(6,1)\|AMMONIA FLASH(6,1)\|AMMONIA MILLION(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(6,1)\|CARBONATE MINERAL(6,1)\|COAL DUST BOILER(6,1)\|COAL FUEL(6,1)\|CONCENTRATED AMMONIA(6,1)\|CORE CARBONATION REACTION(6,1)\|DISSOLVE TARGET(6,1)\|FIN FAN COOLER(6,1)\|FROZEN METAL SILICATE SLURRY(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INSOLUBLE MAGNESIUM HYDROXIDE PRECIPITATION(6,1)\|MAGNESIUM PRECIPITATE(6,1)\|MINE VOID(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PUMPING CAPABILITY(6,1)\|PYROXENE RICH MINERAL(6,1)\|RAW COAL(6,1)\|RAW SLURRY(6,1)\|REACTOR CHOICE(6,1)\|RESIDUAL STEAM(6,1)\|SCRUBBING MEDIA(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE SLURRY DENSITY(6,1)\|SILICATE SLURRY FLOW CARBONATION(6,1)\|TRANSPORTING ORE(6,1)\|FINAL PRODUCT SLURRY(5,4)\|MAGNESIUM CARBONATE(5,4)\|POWER PLANT FLY ASH(5,4)\|PRESSURE EXCHANGE(5,4)\|CONDENSATION(5,3)\|ABSORBER DETAIL(5,2)\|ADJACENT FLOW PATH(5,2)\|CARBON DIOXIDE EMISSION(5,2)\|PRETREATMENT(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AMMONIA RICH SOLUTION(5,1)\|AMMONIA TON HOUR(5,1)\|CARBONATE SILICATE SLURRY(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|CONCENTRIC TUBE(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|FINAL COLD SLURRY FEED(5,1)\|FLASH RECTIFIER VESSEL(5,1)\|FRICTION LOSS(5,1)\|GRADUAL DECREASE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|MILLION KILOWATT HOUR(5,1)\|NATURAL DRAFT COOLING TOWER(5,1)\|PARTICLE CLEANING(5,1)\|PERMANENT PLACEMENT(5,1)\|PREPROCESSING(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|REJUVENATION(5,1)\|SLURRY COOLING(5,1)\|STEAM TON HOUR(5,1)\|STRATEGIC LOCATION(5,1)\|SUPPLEMENTAL HEATING(5,1)\|TUBE BUNDLE(5,1)\|WET GRINDING(5,1)\|JET PUMP(4,4)\|AMBIENT TEMPERATURE(4,3)\|BLACK COAL(4,3)\|EXOTHERMIC REACTION(4,3)\|HYDROSTATIC HEAD(4,3)\|SHELL(4,2)\|SINGLE INTEGRATED(4,2)\|ABSORB REMAINING SENSIBLE HEAT(3,1)\|AIR PREHEATING(3,1)\|ALKALI RICH METAL SILICATE(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA CONTENT(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA RECOVERY VESSEL BOTTOM(3,1)\|AMMONIA RECOVERY VESSEL TOP(3,1)\|AMMONIUM CARBONATE COMPOUND(3,1)\|ARRIVAL PRESSURE(3,1)\|BASEMENT DESIGN(3,1)\|BEDROCK(3,1)\|BOTTOM ASH PULVERIZATION(3,1)\|BULK PRODUCT(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CARBON DIOXIDE ABSORPTION ZONE(3,1)\|CARBON DIOXIDE CAPTURE(3,1)\|CARBON DIOXIDE SCRUBBER CHAMBER(3,1)\|CARBON DIOXIDE SCRUBBING MEDIUM(3,1)\|CARBON DIOXIDE SINK(3,1)\|CARBONHYDROGEN ACID SALT(3,1)\|CHILLED SOLUTION(3,1)\|CLEAN FLUE GAS(3,1)\|COAGULATION(3,1)\|COMMINUTION(3,1)\|CONDUCTING CARBON DIOXIDE(3,1)\|CONSTRUCTED STORAGE COMPARTMENT(3,1)\|COOLER GAS(3,1)\|DESTRUCTION(3,1)\|DOSING(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|\|(IN293376)\|METHANEDIONE(100,57)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,11)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|REACTION SLURRY(92,25)\|METAL SILICATE SLURRY(81,30)\|METAL SILICATE(74,35)\|AMMONIATED SLURRY(73,5)\|REACTOR(53,24)\|PRESSURIZED AMMONIA(50,1)\|ABSORBED METHANEDIONE(47,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(47,1)\|AMMONIA(44,73)\|METAL SILICATE ROCK(43,2)\|METAL CARBONATE(39,9)\|REACTION ENHANCEMENT(35,5)\|CHILLED SLURRY(34,3)\|AMMONIA ABSORPTION CHILLER(31,2)\|AMMONIA RECOVERY VESSEL(30,14)\|FLOW PATH(30,11)\|UNDERGROUND CHAMBER(30,10)\|EVAPORATION CHAMBER(29,1)\|SLURRY(28,41)\|MAGNESIUM SILICATE(25,2)\|AMMONIA WATER(24,16)\|RESIDUAL AMMONIA SCRUBBER(19,4)\|OVERLAND AMMONIA PIPELINE(19,2)\|METAL CARBONATE PRODUCT(16,4)\|CHILLED AMMONIA WATER(16,3)\|LAGGED ABOVEGROUND PIPELINE(16,1)\|METHANEDIONE PERMANENT SEQUESTRATION(16,1)\|RESULTANT AMMONIA WATER(16,1)\|ABSORBENT SLURRY DELUGING SPRAY(15,1)\|MINERAL CARBONATION(14,3)\|AMMONIA ABSORPTION CHAMBER(13,4)\|AMMONIA BUBBLE(13,3)\|HUNTER VALLEY(13,2)\|METHANEDIONE CAPTURE(13,2)\|METHANEDIONE SINK(13,2)\|RESIDUAL METHANEDIONE SCRUBBER(13,1)\|EVAPORATOR CHAMBER(12,5)\|RETURN PIPELINE(12,5)\|CO2 ABSORBER(12,3)\|INSOLUBLE CARBONATE(12,3)\|CARBONATED SILICATE SLURRY(12,1)\|METHANEDIONE TONNE(12,1)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|UNDERGROUND REACTOR(11,2)\|BOILER ECONOMIZER(11,1)\|CHILLED SILICATE SLURRY(11,1)\|FINAL EMPLACEMENT REHABILITATION(11,1)\|INCOMING REACTANT PIPELINE(11,1)\|METHANEDIONE SCRUBBING CHAMBER(11,1)\|SILICATE SLURRY CIRCULATION(11,1)\|RAW FLUE GAS(10,6)\|METHANEDIONE CONTENT(10,2)\|FLUE GAS FILTER(9,5)\|OLIVINE(9,5)\|REACTION SOLUTION(9,5)\|AMMONIA LOSS(9,3)\|ELECTRICITY GENERATION PLANT(9,3)\|EVAPORATOR VESSEL(9,2)\|AMMONIA TONNE(9,1)\|BICARBONATE NH4HCO(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|FIN FAN COOLER(9,1)\|INCOMING SILICATE SLURRY(9,1)\|INSOLUBLE MAGNESIA(9,1)\|MAXIMIZE REGENERATION(9,1)\|METHANEDIONE ABSORPTION ZONE(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OVERLAND PIPELINE(9,1)\|REACTED SLURRY RISING(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(9,1)\|STACKED SUBCHAMBER(9,1)\|CARBON DIOXIDE(8,3)\|AMMONIA STRIPPING(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|PRESSURIZED AMMONIA PASS(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(8,1)\|POWER STATION SITE(7,7)\|CONDENSATION(7,3)\|MAGNESIUM ION(7,2)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|SLURRY FEED(7,2)\|FINAL PRODUCT SLURRY(6,5)\|MWE(6,5)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA MILLION(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBONATE MINERAL(6,1)\|CONCENTRATED AMMONIA(6,1)\|CONCENTRIC PIPE(6,1)\|CORE CARBONATION REACTION(6,1)\|FINAL PERMANENT REPOSITORY(6,1)\|GAS REMNANT(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INORGANIC COMPONENT(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|NATURAL SILICATE(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRETREATMENT EXTENT(6,1)\|PYROXENE RICH MINERAL(6,1)\|PYROXENE SILICATE METAL(6,1)\|RAW SLURRY(6,1)\|REACTED SLURRY RISE(6,1)\|RECOVERED AMMONIA(6,1)\|RESIDUAL VAPOR(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE CONVERSION(6,1)\|SLURRY REACTION(6,1)\|TRANSPORTING ORE(6,1)\|PRESSURE EXCHANGE(5,11)\|BOTTOM ASH PULVERIZATION(5,2)\|DOLOMITE(5,2)\|LIMESTONE(5,2)\|MG3SI2O(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|HOT PRODUCT PIPELINE(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|METHANEDIONE SOURCE(5,1)\|OXIDE REACTION(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|VAPORIZED AMMONIA FLOW(5,1)\|WT SLURRY(5,1)\|REACTION CHAMBER(4,4)\|METAL SILICATE SOLUTION(4,3)\|POWER STATION FLY ASH(4,3)\|SOX(4,3)\|STEAM(4,3)\|INSULATION(4,2)\|AIR PREHEATING(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA PIPE DIAMETER(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SOLUTION(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BEDROCK(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CHESHUNT MIXTURE COMPOUND(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|FINAL CARBONATE PRODUCT SLURRY(4,1)\|\|(IN6026/DELNP/2009)\|METHANEDIONE SEQUESTRATION(100,1)\|REACTION SLURRY(53,2)\|METHANEDIONE(50,3)\|METHANEDIONE SEQUESTRATION(34,1)\|METAL SILICATE ROCK(30,1)\|METAL SILICATE SLURRY(28,1)\|METAL SILICATE(22,1)\|GAS STREAM(21,1)\|REACTOR(20,1)\|METAL CARBONATE(19,1)\|\|(CA2678800)\|METHANEDIONE(100,55)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,10)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|REACTION SLURRY(91,24)\|METAL SILICATE SLURRY(90,30)\|METAL SILICATE(86,37)\|AMMONIATED SLURRY(77,5)\|MAGNESIUM RICH SILICATE(75,8)\|REACTOR(57,23)\|AMMONIA(56,76)\|AMMONIA ABSORPTION RECOVERY VESSEL(50,1)\|METAL CARBONATE(45,10)\|METAL SILICATE ROCK(45,2)\|SLURRY(38,43)\|REACTION ENHANCEMENT(37,5)\|AMMONIA ABSORPTION CHILLER(33,2)\|AMMONIA RECOVERY VESSEL(32,14)\|LIQUID PRESSURIZATION(32,1)\|FLOW PATH(31,11)\|AMMONIA ABSORPTION CHAMBER(30,5)\|OLIVINE(26,7)\|EVAPORATOR CHAMBER(26,6)\|AMMONIA WATER(23,14)\|UNDERGROUND CHAMBER(20,8)\|RESIDUAL AMMONIA SCRUBBER(20,4)\|OVERLAND AMMONIA PIPELINE(20,2)\|RECIRCULATION(20,2)\|LAGGED ABOVEGROUND PIPELINE(19,1)\|METAL CARBONATE PRODUCT(17,4)\|METHANEDIONE PERMANENT SEQUESTRATION(17,1)\|CENT METHANEDIONE(16,2)\|CHAMBER PRODUCT(16,2)\|ABSORBENT SLURRY DELUGING SPRAY(16,1)\|MINERAL CARBONATION(15,3)\|PRODUCING CHAMBER(15,2)\|AMMONIA BUBBLE(14,3)\|HUNTER VALLEY(14,2)\|TARGET METAL(14,2)\|RESIDUAL METHANEDIONE SCRUBBER(14,1)\|RETURN PIPELINE(13,5)\|CARBONATED SILICATE SLURRY(13,1)\|METHANEDIONE TONNE(13,1)\|INSOLUBLE CARBONATE(12,3)\|CHILLED SLURRY(12,2)\|HOT SILICATE SLURRY(12,2)\|INCOMING REACTIVE SLURRY(12,2)\|UNDERGROUND REACTOR(12,2)\|CARBON DIOXIDE(11,3)\|METHANEDIONE CONTENT(11,2)\|BLACK COAL MWE(11,1)\|BOILER ECONOMIZER(11,1)\|CHILLED SILICATE SLURRY(11,1)\|FINAL EMPLACEMENT REHABILITATION(11,1)\|INCOMING REACTANT PIPELINE(11,1)\|METHANEDIONE SCRUBBING CHAMBER(11,1)\|SILICATE SLURRY CIRCULATION(11,1)\|RAW FLUE GAS(10,6)\|AMMONIA LOSS(10,3)\|CARBONATION REACTION(10,2)\|EVAPORATOR VESSEL(10,2)\|FIRED ELECTRICITY GENERATION PLANT(10,2)\|AMMONIA TONNE(10,1)\|DEINKING ASH(10,1)\|ELECTRICITY GWH(10,1)\|FIN FAN COOLER(10,1)\|GLOBAL WARMING METHANEDIONE(10,1)\|INCOMING SILICATE SLURRY(10,1)\|INSOLUBLE MAGNESIA(10,1)\|MAXIMIZE REGENERATION(10,1)\|METHANEDIONE ABSORPTION ZONE(10,1)\|METHANEDIONE SINK(10,1)\|MULTISTAGE BARREL PUMP(10,1)\|OVERLAND PIPELINE(10,1)\|REACTED SLURRY RISING(10,1)\|RESIDUAL AMMONIA ABSORBER(10,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(10,1)\|STACKED SUBCHAMBER(10,1)\|FLUE GAS FILTER(9,5)\|REACTION SOLUTION(9,5)\|MINERAL MATTER(8,2)\|PUMPING ENERGY(8,2)\|SLURRY FEED(8,2)\|ABSORBER AQ(8,1)\|AMMONIA STRIPPING(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|HOT PRESSURIZED FMAL PRODUCT(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|PRESSURIZED AMMONIA PASS(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(8,1)\|POWER STATION SITE(7,7)\|CONDENSATION(7,3)\|ABSORB SURPLUS SENSIBLE HEAT(7,1)\|ALKALINE INDUSTRY RESIDUE(7,1)\|AMMONIA MILLION(7,1)\|BOOSTER PUMPING STATION(7,1)\|CARBONATE MINERAL(7,1)\|CONCENTRATED AMMONIA(7,1)\|CONCENTRIC PIPE(7,1)\|FINAL PERMANENT REPOSITORY(7,1)\|GAS REMNANT(7,1)\|GEHO PUMP(7,1)\|HOT SLURRY RISING(7,1)\|INORGANIC COMPONENT(7,1)\|MINE SITE(7,1)\|MINE VOID(7,1)\|MOIL CO2(7,1)\|MOLL CO2(7,1)\|NATURAL SILICATE(7,1)\|PAPER RECYCLING RESIDUE COMBUSTION(7,1)\|PIPELINE REACTOR CHOICE(7,1)\|PRETREATMENT EXTENT(7,1)\|PYROXENE RICH MINERAL(7,1)\|PYROXENE SILICATE METAL(7,1)\|RAW SLURRY(7,1)\|REACTED SLURRY RISE(7,1)\|RESIDUAL VAPOR(7,1)\|SCRUBBING ZONE(7,1)\|SILICATE CONVERSION(7,1)\|SLURRY REACTION(7,1)\|TRANSPORTING ORE(7,1)\|PRESSURE EXCHANGE(6,10)\|ADJACENT FLOW PATH(6,2)\|BOTTOM ASH PULVERIZATION(6,2)\|CHILLED AMMONIA WATER(6,2)\|DOLOMITE(6,2)\|LIMESTONE(6,2)\|WOLLASTONITE(6,2)\|FINAL PRODUCT SLURRY(5,4)\|REACTION CHAMBER(5,4)\|METAL SILICATE SOLUTION(5,3)\|POWER STATION FLY ASH(5,3)\|SOX(5,3)\|STEAM(5,3)\|INSULATION(5,2)\|SHELL(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|HOT PRODUCT PIPELINE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|METHANEDIONE SOURCE(5,1)\|OXIDE REACTION(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|VAPORIZED AMMONIA FLOW(5,1)\|WT SLURRY(5,1)\|AIR PREHEATING(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA PIPE DIAMETER(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SOLUTION(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CHESHUNT MIXTURE COMPOUND(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|\|(CA2678800)\|METHANEDIONE(100,55)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,10)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|REACTION SLURRY(91,24)\|METAL SILICATE SLURRY(90,30)\|METAL SILICATE(86,37)\|AMMONIATED SLURRY(77,5)\|MAGNESIUM RICH SILICATE(75,8)\|REACTOR(57,23)\|AMMONIA(56,76)\|AMMONIA ABSORPTION RECOVERY VESSEL(50,1)\|METAL CARBONATE(45,10)\|METAL SILICATE ROCK(45,2)\|SLURRY(38,43)\|REACTION ENHANCEMENT(37,5)\|AMMONIA ABSORPTION CHILLER(33,2)\|AMMONIA RECOVERY VESSEL(32,14)\|LIQUID PRESSURIZATION(32,1)\|FLOW PATH(31,11)\|AMMONIA ABSORPTION CHAMBER(30,5)\|OLIVINE(26,7)\|EVAPORATOR CHAMBER(26,6)\|AMMONIA WATER(23,14)\|UNDERGROUND CHAMBER(20,8)\|RESIDUAL AMMONIA SCRUBBER(20,4)\|OVERLAND AMMONIA PIPELINE(20,2)\|RECIRCULATION(20,2)\|LAGGED ABOVEGROUND PIPELINE(19,1)\|METAL CARBONATE PRODUCT(17,4)\|METHANEDIONE PERMANENT SEQUESTRATION(17,1)\|CENT METHANEDIONE(16,2)\|CHAMBER PRODUCT(16,2)\|ABSORBENT SLURRY DELUGING SPRAY(16,1)\|MINERAL CARBONATION(15,3)\|PRODUCING CHAMBER(15,2)\|AMMONIA BUBBLE(14,3)\|HUNTER VALLEY(14,2)\|TARGET METAL(14,2)\|RESIDUAL METHANEDIONE SCRUBBER(14,1)\|RETURN PIPELINE(13,5)\|CARBONATED SILICATE SLURRY(13,1)\|METHANEDIONE TONNE(13,1)\|INSOLUBLE CARBONATE(12,3)\|CHILLED SLURRY(12,2)\|HOT SILICATE SLURRY(12,2)\|INCOMING REACTIVE SLURRY(12,2)\|UNDERGROUND REACTOR(12,2)\|CARBON DIOXIDE(11,3)\|METHANEDIONE CONTENT(11,2)\|BLACK COAL MWE(11,1)\|BOILER ECONOMIZER(11,1)\|CHILLED SILICATE SLURRY(11,1)\|FINAL EMPLACEMENT REHABILITATION(11,1)\|INCOMING REACTANT PIPELINE(11,1)\|METHANEDIONE SCRUBBING CHAMBER(11,1)\|SILICATE SLURRY CIRCULATION(11,1)\|RAW FLUE GAS(10,6)\|AMMONIA LOSS(10,3)\|CARBONATION REACTION(10,2)\|EVAPORATOR VESSEL(10,2)\|FIRED ELECTRICITY GENERATION PLANT(10,2)\|AMMONIA TONNE(10,1)\|DEINKING ASH(10,1)\|ELECTRICITY GWH(10,1)\|FIN FAN COOLER(10,1)\|GLOBAL WARMING METHANEDIONE(10,1)\|INCOMING SILICATE SLURRY(10,1)\|INSOLUBLE MAGNESIA(10,1)\|MAXIMIZE REGENERATION(10,1)\|METHANEDIONE ABSORPTION ZONE(10,1)\|METHANEDIONE SINK(10,1)\|MULTISTAGE BARREL PUMP(10,1)\|OVERLAND PIPELINE(10,1)\|REACTED SLURRY RISING(10,1)\|RESIDUAL AMMONIA ABSORBER(10,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(10,1)\|STACKED SUBCHAMBER(10,1)\|FLUE GAS FILTER(9,5)\|REACTION SOLUTION(9,5)\|MINERAL MATTER(8,2)\|PUMPING ENERGY(8,2)\|SLURRY FEED(8,2)\|ABSORBER AQ(8,1)\|AMMONIA STRIPPING(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|HOT PRESSURIZED FMAL PRODUCT(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|PRESSURIZED AMMONIA PASS(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(8,1)\|POWER STATION SITE(7,7)\|CONDENSATION(7,3)\|ABSORB SURPLUS SENSIBLE HEAT(7,1)\|ALKALINE INDUSTRY RESIDUE(7,1)\|AMMONIA MILLION(7,1)\|BOOSTER PUMPING STATION(7,1)\|CARBONATE MINERAL(7,1)\|CONCENTRATED AMMONIA(7,1)\|CONCENTRIC PIPE(7,1)\|FINAL PERMANENT REPOSITORY(7,1)\|GAS REMNANT(7,1)\|GEHO PUMP(7,1)\|HOT SLURRY RISING(7,1)\|INORGANIC COMPONENT(7,1)\|MINE SITE(7,1)\|MINE VOID(7,1)\|MOIL CO2(7,1)\|MOLL CO2(7,1)\|NATURAL SILICATE(7,1)\|PAPER RECYCLING RESIDUE COMBUSTION(7,1)\|PIPELINE REACTOR CHOICE(7,1)\|PRETREATMENT EXTENT(7,1)\|PYROXENE RICH MINERAL(7,1)\|PYROXENE SILICATE METAL(7,1)\|RAW SLURRY(7,1)\|REACTED SLURRY RISE(7,1)\|RESIDUAL VAPOR(7,1)\|SCRUBBING ZONE(7,1)\|SILICATE CONVERSION(7,1)\|SLURRY REACTION(7,1)\|TRANSPORTING ORE(7,1)\|PRESSURE EXCHANGE(6,10)\|ADJACENT FLOW PATH(6,2)\|BOTTOM ASH PULVERIZATION(6,2)\|CHILLED AMMONIA WATER(6,2)\|DOLOMITE(6,2)\|LIMESTONE(6,2)\|WOLLASTONITE(6,2)\|FINAL PRODUCT SLURRY(5,4)\|REACTION CHAMBER(5,4)\|METAL SILICATE SOLUTION(5,3)\|POWER STATION FLY ASH(5,3)\|SOX(5,3)\|STEAM(5,3)\|INSULATION(5,2)\|SHELL(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|HOT PRODUCT PIPELINE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|METHANEDIONE SOURCE(5,1)\|OXIDE REACTION(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|VAPORIZED AMMONIA FLOW(5,1)\|WT SLURRY(5,1)\|AIR PREHEATING(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA PIPE DIAMETER(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SOLUTION(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CHESHUNT MIXTURE COMPOUND(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|\|(KR10-1527365)\|CARBON DIOXIDE(100,110)\|REACTION SLURRY(100,30)\|CARBON DIOXIDE ISOLATION(100,9)\|CARBON DIOXIDE SEQUESTRATION(100,8)\|GAS STREAM(100,7)\|METAL SILICATE(88,47)\|REACTOR(72,26)\|METAL SILICATE SLURRY(64,30)\|SLURRY(48,44)\|METAL CARBONATE(47,12)\|AMMONIA(46,70)\|MAGNESIUM RICH SILICATE(46,7)\|AMMONIA ABSORPTION RECOVERY VESSEL(46,1)\|METAL AMMINE FAILURE(45,1)\|METALSILICATE(45,1)\|METAL AMMINE(40,1)\|REACTION ENHANCEMENT(38,6)\|INSOLUBLE CARBONATE(35,4)\|METAL SILICATE ROCK(35,4)\|ABSORB CARBON DIOXIDE(35,1)\|DISPERSED METAL SILICATE(35,1)\|RECOVERING AMMONIA(33,2)\|SEPARATING CARBON DIOXIDE(33,1)\|FLOW PATH(31,17)\|AMMONIA ABSORPTION CHAMBER(28,6)\|CHAMBER PRESSURIZATION(28,1)\|AMMONIA WATER(23,19)\|METER(23,1)\|NATURALLY OCCURRING ABSORPTION SOURCE(23,1)\|WHOLITE(22,1)\|CLEANING CHAMBER(21,19)\|RESIDUAL AMMONIA SCRUBBER(19,4)\|AMMONIA WATER SLURRY(19,1)\|GRINDING(19,1)\|AMMONIA RECOVERY VESSEL(18,5)\|OLIVINE(17,6)\|REACTOR CONTROL(17,5)\|METAL CARBONATE PRODUCT(17,3)\|AMMONIATED CARBONATED SILICATE SLURRY(17,1)\|CARBON DIOXIDE CHANGE(17,1)\|POWER DIRECTED EMESIS(17,1)\|SUBTERRANEAN CHAMBER(16,6)\|GRAPHITIC BURNING ELECTROGENIC GENERATOR(16,1)\|CARBON DIOXIDE REACTION(15,1)\|MINERAL CARBONIZATION(14,3)\|MINERAL SERPENTINE MG3SI2O(13,1)\|PULVERULENT COMBUSTION BOILER(13,1)\|HEAT EXCHANGER(12,24)\|AMMONIA GAS RECOVERY VESSEL(12,9)\|EVAPORATOR CHAMBER(12,5)\|RETURN PIPELINE(12,5)\|AMMONIA LOSS(11,5)\|HOT SILICATE SLURRY(11,2)\|HUNTER VALLEY(11,2)\|SUBTERRANEAN REACTOR(11,2)\|ABSORPTION SLURRY OVERFLOW SPRAY(11,1)\|BOILER ECONOMIZER(11,1)\|DESIRED TRANSFER(11,1)\|GRAPHITIC COMBUSTION GENERATOR(11,1)\|INTRODUCTION REACTANT PIPELINE(11,1)\|SILICATE SLURRY CIRCULATION(11,1)\|FLUE GAS(10,33)\|AMMONIA BUBBLE(10,2)\|CO2 ABSORBER(10,2)\|FLUE GAS FILTER(9,5)\|TONNE(9,5)\|POWER PLANT FLUE GAS(9,4)\|EVAPORATOR VESSEL(9,2)\|AMMONIA ABSORPTION COOLER(9,1)\|ELECTRICITY GWH(9,1)\|HEAT DESIRED TRANSFER(9,1)\|LIME CALCINATION(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|STACKED SUBCHAMBER(9,1)\|SUDDEN EVAPORATION RECTIFICATION VESSEL(9,1)\|POWER PLANT(8,22)\|REACTION SOLUTION(8,5)\|DOLOMITE(8,4)\|RAW FLUE GAS(8,4)\|HOT SLURRY(8,3)\|LIMESTONE(8,3)\|PERMANENT INSULATION(8,2)\|3T M3 SLURRY(8,1)\|AMMONIA CATALYSIS(8,1)\|AMMONIA PIPELINE(8,1)\|AMMONIA STRIPPING(8,1)\|COLD SILICATE SLURRY(8,1)\|COOLED SILICATE SLURRY(8,1)\|DEINKING ASH(8,1)\|ELEMENTAL IRON FE(8,1)\|KEY CARBONIZATION(8,1)\|LJUNGSTROM ROTARY(8,1)\|MULTISTAGE BARRIER(8,1)\|RAW REACTION SLURRY(8,1)\|ULTRA MAFIC ROCK(8,1)\|CARBON DIOXIDE SEPARATOR(7,3)\|WOLLASTONITE(7,3)\|ABSORPTION ZONE(7,2)\|CARBON DIOXIDE SEQUESTRANT(7,2)\|COUNTERCURRENT(7,2)\|PUMPING ENERGY(7,2)\|AMMONIUM SALT(6,2)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMINE FORMATION(6,1)\|AMMONIA BULK(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON ISOLATION ENERGY BURDEN(6,1)\|CARBONATE MINERAL(6,1)\|CLEAN SUPERNATANT(6,1)\|CLEANING MEDIUM CIRCULATION(6,1)\|CONCENTRIC PIPE(6,1)\|DISSOLVE TARGET(6,1)\|ELECTROMAGNETIC PRECIPITATE(6,1)\|ENERGY MWT(6,1)\|FIN FAN(6,1)\|FINE UNDERGROUND CHAMBER(6,1)\|GEHO PUMP(6,1)\|GENERATOR FIRING(6,1)\|GRADUAL MANNER RESULT(6,1)\|INTRODUCED REACTIVE SLURRY(6,1)\|INTRODUCED SILICATE SLURRY(6,1)\|MAGNESIUM DISSOLUTION(6,1)\|MEGAWATT HOUR TON(6,1)\|MILD REAGENT(6,1)\|MILLION AMMONIA(6,1)\|MINING SITE(6,1)\|MWE COAL(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PARTICULATE CLEANING(6,1)\|RAW SLURRY(6,1)\|RICH MINERAL(6,1)\|SILICATE SLURRY DENSITY(6,1)\|SITE CARBONIZATION(6,1)\|SLURRY REACTION(6,1)\|SUBTERRANEAN PROCESSING VESSEL(6,1)\|THROTTLING VALVE(6,1)\|TOTALITY PRODUCT SLURRY(6,1)\|WATER ABSORBENT(6,1)\|POWER PLANT SITE(5,4)\|CARBON DIOXIDE EMISSION(5,2)\|DOLIME(5,2)\|LIPID CONDITION(5,2)\|AMMONIA COMBINED SLURRY(5,1)\|CALCIUM CA(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENTRIFUGAL PUMP FORMAT(5,1)\|CIRCULATION ENOUGH NATURAL PROPORTION(5,1)\|CLASSIFICATION(5,1)\|COAL FUEL(5,1)\|COLD SLURRY(5,1)\|COOLED SLURRY(5,1)\|DIVALENT IRON(5,1)\|EMISSION END(5,1)\|FINAL INSTALLATION SITE(5,1)\|FINAL PERMANENT RESERVOIR(5,1)\|FLOOR ASH(5,1)\|FRICTION LOSS(5,1)\|GENERATOR SITE(5,1)\|GROUND AMMONIA(5,1)\|GROUND PIPELINE(5,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(5,1)\|MAGNESIUM CARBONATE EXTRACTION(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM MG(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|MAXIMIZE GENERATION(5,1)\|ORE SITE(5,1)\|PERMANENT PLACEMENT(5,1)\|PIPE REACTOR(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PRETREATMENT EXTENT(5,1)\|PUMPING CAPACITY(5,1)\|RESIDUAL VAPOR(5,1)\|SERPENTINE MINERAL ACID SITE(5,1)\|SLOW IDEAL(5,1)\|SLURRY COOLING(5,1)\|SLURRY FEED(5,1)\|STATIONARY PLANT(5,1)\|STRATEGIC LOCATION(5,1)\|STRIP AMMONIA(5,1)\|THICK SLURRY(5,1)\|UNDERGOING TREATMENT(5,1)\|CARBON DIOXIDE SEQUESTRATION(4,3)\|FINAL PRODUCT SLURRY(4,3)\|METAL SILICATE SOLUTION(4,3)\|SOX(4,3)\|ULTRASOUND(4,3)\|2CO3AMMONIA(4,1)\|2CO3BASED(4,1)\|ABSORB EXCESS SENSIBLE HEAT(4,1)\|AMMONIA GAS BUBBLE(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA PIPE DIAMETER(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SALT SOLUTION(4,1)\|AMMONIUM CARBONATE COMPOUND(4,1)\|ANNULUS(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BOTTOM ASH PULVERIZATION(4,1)\|CARBAMATE(4,1)\|CARBON DIOXIDE CLEANING CHAMBER(4,1)\|CARBON DIOXIDE PERMANENT ISOLATION(4,1)\|CARBON DIOXIDE SCRUBBER(4,1)\|CARBON DIOXIDE SINK(4,1)\|CASIO3PAUL(4,1)\|CLEAN FLUE GAS(4,1)\|CLEANING REGION(4,1)\|CM3WILL(4,1)\|CONCENTRIC INNER(4,1)\|CONTINENT(4,1)\|CRUSHING(4,1)\|DOWNSTREAM GAS(4,1)\|ECONOMIC PERSPECTIVE(4,1)\|EXOTHERMIC CARBON DIOXIDE(4,1)\|\|(KR10-2009-0125109)\|CARBON DIOXIDE(100,114)\|AMMONIA(100,72)\|METAL SILICATE(100,54)\|SLURRY(100,47)\|METAL SILICATE SLURRY(100,35)\|PIPELINE(100,35)\|REACTION SLURRY(100,33)\|AMMONIA WATER(100,22)\|METAL CARBONATE(100,15)\|CARBON DIOXIDE SEQUESTRATION(100,9)\|EVAPORATOR(100,8)\|ABSORPTION(100,6)\|METAL SILICATE ROCK(100,5)\|AMMONIA ABSORPTION(100,4)\|CARBON DIOXIDE SEQUESTRATION(100,4)\|GAS STREAM(100,4)\|METAL SILICATE ROCK SLURRY(100,4)\|SEQUESTRATION(100,4)\|ABSORPTION(100,1)\|COOLING PATTERN(100,1)\|LIQUID PRESSURIZATION(100,1)\|AMMONIATED SLURRY(72,1)\|MAGNESIUM RICH SILICATE(68,9)\|REACTOR(56,24)\|REACTION ENHANCEMENT(41,7)\|DISSOLVE TARGET(40,2)\|AMMONIA ABSORPTION RECOVERY VESSEL(40,1)\|METAL AMMINE FAILURE(39,1)\|AMMONIA ABSORPTION COOLER(35,2)\|AMMONIA ABSORPTION CHAMBER(34,7)\|METAL AMMINE(34,1)\|INSOLUBLE CARBONATE(30,4)\|AMMONIA SALT(30,3)\|ABSORB CARBON DIOXIDE(30,1)\|DISPERSED METAL SILICATE(30,1)\|RECOVERING AMMONIA(28,2)\|FLOW PATH(27,14)\|REACTOR CONTROL(26,6)\|SEQUESTRATION CARBON DIOXIDE(24,1)\|CLEANING CHAMBER(23,20)\|AMMONIA LOSS(23,6)\|AMMONIA COMBINED SLURRY(23,2)\|GRINDING(23,2)\|EVAPORATOR CHAMBER(21,6)\|COOLED SLURRY(21,2)\|OLIVINE(20,7)\|CARBON SEQUESTRATION(20,6)\|METER(20,1)\|NATURALLY OCCURRING ABSORPTION SOURCE(20,1)\|WHISTONITE(20,1)\|CARBON DIOXIDE ISOLATION(17,8)\|HEAT EXCHANGER(16,26)\|RESIDUAL AMMONIA SCRUBBER(16,4)\|TARGET METAL(16,4)\|AMMONIA METAL SILICATE SLURRY(16,2)\|AMMONIA RECOVERY VESSEL(15,5)\|METAL CARBONATE PRODUCT(15,3)\|SILICATE METAL(15,2)\|AMMONIATED CARBONATED SILICATE SLURRY(15,1)\|CARBON DIOXIDE CHANGE(15,1)\|POWER DIRECTED EMESIS(15,1)\|SUBTERRANEAN CHAMBER(14,6)\|GRAPHITIC BURNING ELECTROGENIC GENERATOR(14,1)\|CHAMBER PRODUCT(13,2)\|MINERAL CARBONIZATION(12,3)\|PRODUCING CHAMBER(12,2)\|CARBON SEQUESTRATION(11,3)\|MINERAL SERPENTINE MG3SI2O(11,1)\|PULVERULENT COMBUSTION BOILER(11,1)\|FLUE GAS(10,34)\|POWER PLANT(10,24)\|AMMONIA GAS RECOVERY VESSEL(10,9)\|RETURN PIPELINE(10,5)\|COOLED AMMONIA WATER(10,3)\|HOT SILICATE SLURRY(10,2)\|HUNTER VALLEY(10,2)\|SUBTERRANEAN REACTOR(10,2)\|AMMONIA BUBBLE(9,2)\|CO2 ABSORBER(9,2)\|ABSORPTION SLURRY OVERFLOW SPRAY(9,1)\|BOILER ECONOMIZER(9,1)\|DESIRED TRANSFER(9,1)\|GRAPHITIC COMBUSTION GENERATOR(9,1)\|INTRODUCTION REACTANT PIPELINE(9,1)\|SILICATE SLURRY CIRCULATION(9,1)\|POWER PLANT FLUE GAS(8,4)\|EVAPORATOR VESSEL(8,2)\|ELECTRICITY GWH(8,1)\|HEAT DESIRED TRANSFER(8,1)\|LIME CALCINATION(8,1)\|RESIDUAL AMMONIA ABSORBER(8,1)\|STACKED SUBCHAMBER(8,1)\|SUDDEN EVAPORATION RECTIFICATION VESSEL(8,1)\|FLUE GAS FILTER(7,5)\|TONNE(7,5)\|DOLOMITE(7,4)\|RAW FLUE GAS(7,4)\|HOT SLURRY(7,3)\|LIMESTONE(7,3)\|PERMANENT INSULATION(7,2)\|3T M3 SLURRY(7,1)\|AMMONIA CATALYSIS(7,1)\|AMMONIA PIPELINE(7,1)\|AMMONIA STRIPPING(7,1)\|COLD SILICATE SLURRY(7,1)\|COOLED SILICATE SLURRY(7,1)\|DEINKING ASH(7,1)\|ELEMENTAL IRON FE(7,1)\|KEY CARBONIZATION(7,1)\|LJUNGSTROM ROTARY(7,1)\|MULTISTAGE BARRIER(7,1)\|RAW REACTION SLURRY(7,1)\|ULTRA MAFIC ROCK(7,1)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE SEPARATOR(6,3)\|REACTION STEP(6,3)\|WOLLASTONITE(6,3)\|ABSORPTION ZONE(6,2)\|CARBON DIOXIDE SEQUESTRANT(6,2)\|PUMPING ENERGY(6,2)\|AMMONIUM SALT(5,2)\|CARBON DIOXIDE EMISSION(5,2)\|COUNTERCURRENT(5,2)\|DOLIME(5,2)\|LIPID CONDITION(5,2)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMINE FORMATION(5,1)\|AMMONIA BULK(5,1)\|AMMONIA SLIP(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBON ISOLATION ENERGY BURDEN(5,1)\|CARBONATE MINERAL(5,1)\|CLEAN SUPERNATANT(5,1)\|CLEANING MEDIUM CIRCULATION(5,1)\|CONCENTRIC PIPE(5,1)\|ELECTROMAGNETIC PRECIPITATE(5,1)\|ENERGY MWT(5,1)\|FINE UNDERGROUND CHAMBER(5,1)\|GEHO PUMP(5,1)\|GENERATOR FIRING(5,1)\|GRADUAL MANNER RESULT(5,1)\|INTRODUCED REACTIVE SLURRY(5,1)\|INTRODUCED SILICATE SLURRY(5,1)\|MAGNESIUM DISSOLUTION(5,1)\|MEGAWATT HOUR TON(5,1)\|MILD REAGENT(5,1)\|MILLION AMMONIA(5,1)\|MINING SITE(5,1)\|MWE COAL(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PARTICULATE CLEANING(5,1)\|RAW SLURRY(5,1)\|RICH MINERAL(5,1)\|SILICATE SLURRY DENSITY(5,1)\|SITE CARBONIZATION(5,1)\|SLURRY REACTION(5,1)\|SUBTERRANEAN PROCESSING VESSEL(5,1)\|THROTTLING VALVE(5,1)\|TOTALITY PRODUCT SLURRY(5,1)\|WATER ABSORBENT(5,1)\|LIQUID STATE(4,5)\|OVERCOAT(4,4)\|POWER PLANT SITE(4,4)\|FINAL PRODUCT SLURRY(4,3)\|METAL SILICATE SOLUTION(4,3)\|SOX(4,3)\|AGITATION(4,2)\|CALCIUM CA(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENTRIFUGAL PUMP FORMAT(4,1)\|CIRCULATION ENOUGH NATURAL PROPORTION(4,1)\|CLASSIFICATION(4,1)\|COAL FUEL(4,1)\|COLD SLURRY(4,1)\|DIVALENT IRON(4,1)\|EMISSION END(4,1)\|FINAL INSTALLATION SITE(4,1)\|FINAL PERMANENT RESERVOIR(4,1)\|FLOOR ASH(4,1)\|FRICTION LOSS(4,1)\|GENERATOR SITE(4,1)\|GROUND AMMONIA(4,1)\|GROUND PIPELINE(4,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(4,1)\|MAGNESIUM CARBONATE EXTRACTION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM MG(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAXIMIZE GENERATION(4,1)\|ORE SITE(4,1)\|OXIDE REACTION(4,1)\|PERMANENT PLACEMENT(4,1)\|PIPE REACTOR(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PRETREATMENT EXTENT(4,1)\|PUMPING CAPACITY(4,1)\|RESIDUAL VAPOR(4,1)\|SERPENTINE MINERAL ACID SITE(4,1)\|SLOW IDEAL(4,1)\|SLURRY COOLING(4,1)\|SLURRY FEED(4,1)\|STATIONARY PLANT(4,1)\|STRATEGIC LOCATION(4,1)\|STRIP AMMONIA(4,1)\|THICK SLURRY(4,1)\|UNDERGOING TREATMENT(4,1)\|REACTION CHAMBER(3,4)\|2CO3AMMONIA(3,1)\|2CO3BASED(3,1)\|ABSORB EXCESS SENSIBLE HEAT(3,1)\|AMMONIA GAS BUBBLE(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SALT SOLUTION(3,1)\|AMMONIUM CARBONATE COMPOUND(3,1)\|ANNULUS(3,1)\|BAYSWATER POWER STATION(3,1)\|BICARBONATE(3,1)\|BIOMASS(3,1)\|BOTTOM ASH PULVERIZATION(3,1)\|CARBAMATE(3,1)\|CARBON DIOXIDE CLEANING CHAMBER(3,1)\|CARBON DIOXIDE PERMANENT ISOLATION(3,1)\|CARBON DIOXIDE SCRUBBER(3,1)\|CARBON DIOXIDE SINK(3,1)\|CASIO3PAUL(3,1)\|CLEAN FLUE GAS(3,1)\|CLEANING REGION(3,1)\|CM3WILL(3,1)\|\|(AU2008217572)\|METAL SILICATE SLURRY(100,32)\|REACTION SLURRY(92,24)\|METAL SILICATE(80,38)\|LIMESTONE PULVERIZATION(79,1)\|AMMONIATED SLURRY(71,5)\|METAL CARBONATE(68,13)\|MAGNESIUM RICH SILICATE(61,7)\|PERMANENT SEQUESTRATION(55,2)\|REACTOR(52,25)\|REACTION ENHANCEMENT(51,6)\|SEQUESTERING CARBON DIOXIDE(51,3)\|COAL FUEL(51,1)\|CARBON DIOXIDE(50,66)\|PIPELINE(50,28)\|SLURRY(45,43)\|GAS STREAM(45,11)\|AMMONIA ABSORPTION RECOVERY VESSEL(45,1)\|FLOW PATH(43,12)\|AMMONIA(41,66)\|RECOVERING AMMONIA(40,8)\|NATURALLY OCCURRING SINK(40,1)\|SCRUBBING CHAMBER(37,17)\|INSOLUBLE CARBONATE(35,4)\|POWER THIRSTY CLIMATE(35,1)\|RETURN PATHWAY(34,2)\|DOLOMITE(33,4)\|AMMONIA ABSORPTION CHILLER(31,2)\|CARBON SEQUESTRATION(29,9)\|AMMONIA WATER(28,13)\|REACTOR CONTROL(28,1)\|POWER STATION BOILER(26,1)\|METAL SILICATE ROCK(22,2)\|SEQUESTER CARBON DIOXIDE(22,2)\|CARBON SEQUESTRATION(21,3)\|CARBON DIOXIDE REMOVAL(21,2)\|UNDERGROUND CHAMBER(20,9)\|DUTY(20,2)\|AMMONIA RECOVERY VESSEL(19,14)\|OVERLAND AMMONIA PIPELINE(19,2)\|CARBON DIOXIDE SEQUESTRATION(18,23)\|PRESSURIZED LIQUID AMMONIA(18,3)\|OLIVINE(17,6)\|CARBON CAPTURE(17,1)\|LAGGED ABOVEGROUND PIPELINE(17,1)\|FLY ASH(15,7)\|AMMONIA ABSORPTION CHAMBER(15,5)\|POWER STATION FLY ASH(15,4)\|CHAMBER PRODUCT(15,2)\|POWER STATION(14,26)\|PRODUCING CHAMBER(14,2)\|ABSORBENT SLURRY DELUGING SPRAY(14,1)\|MINERAL CARBONATION(13,3)\|HUNTER VALLEY(13,2)\|CARBON DIOXIDE SEQUESTRATION(12,7)\|EVAPORATOR CHAMBER(12,5)\|RETURN PIPELINE(12,5)\|ABSORBING AMMONIA(12,3)\|CARBONATED SILICATE SLURRY(12,1)\|CHILLED SLURRY(11,2)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|UNDERGROUND REACTOR(11,2)\|BLACK COAL MWE(10,1)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|INCOMING REACTANT PIPELINE(10,1)\|SILICATE SLURRY CIRCULATION(10,1)\|RAW FLUE GAS(9,6)\|FLUE GAS FILTER(9,5)\|REACTION SOLUTION(9,5)\|CARBONATION REACTION(9,2)\|EVAPORATOR VESSEL(9,2)\|FIRED ELECTRICITY GENERATION PLANT(9,2)\|AMMONIA TONNE(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|INCOMING SILICATE SLURRY(9,1)\|MAXIMIZE REGENERATION(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OVERLAND PIPELINE(9,1)\|REACTED SLURRY RISING(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|STACKED SUBCHAMBER(9,1)\|ABSORBER AQ(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HOT PRESSURIZED FMAL PRODUCT(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|RAW REACTIVE SLURRY(8,1)\|TONNE AMMONIA(8,1)\|POWER STATION SITE(7,7)\|CARBON DIOXIDE TONNE(7,2)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|SLURRY FEED(7,2)\|CONDENSATION(6,3)\|CENT CARBON DIOXIDE(6,2)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA CONCENTRATION(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(6,1)\|CARBONATE MINERAL FINAL EMPLACEMENT(6,1)\|CONCENTRIC PIPE(6,1)\|FINAL PERMANENT REPOSITORY(6,1)\|GAS REMNANT(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INORGANIC COMPONENT(6,1)\|INSOLUBLE CARBONATE NATURE(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|NATURAL SILICATE(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRETREATMENT EXTENT(6,1)\|PYROXENE RICH MINERAL(6,1)\|PYROXENE SILICATE METAL(6,1)\|RAW SLURRY(6,1)\|REACTED SLURRY RISE(6,1)\|RESIDUAL VAPOR(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE CONVERSION(6,1)\|SLURRY REACTION(6,1)\|TRANSPORTING ORE(6,1)\|FINAL PRODUCT SLURRY(5,4)\|ADJACENT FLOW PATH(5,2)\|BOTTOM ASH PULVERIZATION(5,2)\|CHILLED AMMONIA WATER(5,2)\|LIMESTONE(5,2)\|RESIDUAL AMMONIA SCRUBBER DETAIL(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|AMMONIA VAPOR FLOW(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|HOT PRODUCT PIPELINE(5,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(5,1)\|KEEPING UP(5,1)\|LIQUID PRESSURIZATION(5,1)\|MAGNESIUM CARBONATE EXTRACTION(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|OXIDE REACTION(5,1)\|PERFOI RING(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|WT SLURRY(5,1)\|AMMONIUM SALT(4,4)\|REACTION CHAMBER(4,4)\|SOX(4,3)\|INSULATION(4,2)\|LIQUID AMMONIA RECOVERY(4,2)\|SHELL(4,2)\|SINGLE INTEGRATED(4,2)\|AIR PREHEATING(4,1)\|AMMONIA ABSORBER(4,1)\|AMMONIA GAS PIPE DIAMETER(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIUM CARBONATE COMPOUND(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CARBON DIOXIDE ABSORPTION ZONE(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|GAS LIQUID SEPARATOR(4,1)\|GEOLOGICAL CONDITION PERMIT(4,1)\|HARMFUL CARBON DIOXIDE GAS(4,1)\|HEAT BALANCE FIGURE(4,1)\|HEAT CONSERVATION(4,1)\|ID MOL(4,1)\|INDICATIVE MASS(4,1)\|LATTER CONTINUING(4,1)\|LIDDELL POWER STATION(4,1)\|\|(AU2008217572)\|METAL SILICATE SLURRY(100,32)\|REACTION SLURRY(92,24)\|METAL SILICATE(80,38)\|LIMESTONE PULVERIZATION(79,1)\|AMMONIATED SLURRY(71,5)\|METAL CARBONATE(68,13)\|MAGNESIUM RICH SILICATE(61,7)\|PERMANENT SEQUESTRATION(55,2)\|REACTOR(52,25)\|REACTION ENHANCEMENT(51,6)\|SEQUESTERING CARBON DIOXIDE(51,3)\|COAL FUEL(51,1)\|CARBON DIOXIDE(50,66)\|PIPELINE(50,28)\|SLURRY(45,43)\|GAS STREAM(45,11)\|AMMONIA ABSORPTION RECOVERY VESSEL(45,1)\|FLOW PATH(43,12)\|AMMONIA(41,66)\|RECOVERING AMMONIA(40,8)\|NATURALLY OCCURRING SINK(40,1)\|SCRUBBING CHAMBER(37,17)\|INSOLUBLE CARBONATE(35,4)\|POWER THIRSTY CLIMATE(35,1)\|RETURN PATHWAY(34,2)\|DOLOMITE(33,4)\|AMMONIA ABSORPTION CHILLER(31,2)\|CARBON SEQUESTRATION(29,9)\|AMMONIA WATER(28,13)\|REACTOR CONTROL(28,1)\|POWER STATION BOILER(26,1)\|METAL SILICATE ROCK(22,2)\|SEQUESTER CARBON DIOXIDE(22,2)\|CARBON SEQUESTRATION(21,3)\|CARBON DIOXIDE REMOVAL(21,2)\|UNDERGROUND CHAMBER(20,9)\|DUTY(20,2)\|AMMONIA RECOVERY VESSEL(19,14)\|OVERLAND AMMONIA PIPELINE(19,2)\|CARBON DIOXIDE SEQUESTRATION(18,23)\|PRESSURIZED LIQUID AMMONIA(18,3)\|OLIVINE(17,6)\|CARBON CAPTURE(17,1)\|LAGGED ABOVEGROUND PIPELINE(17,1)\|FLY ASH(15,7)\|AMMONIA ABSORPTION CHAMBER(15,5)\|POWER STATION FLY ASH(15,4)\|CHAMBER PRODUCT(15,2)\|POWER STATION(14,26)\|PRODUCING CHAMBER(14,2)\|ABSORBENT SLURRY DELUGING SPRAY(14,1)\|MINERAL CARBONATION(13,3)\|HUNTER VALLEY(13,2)\|CARBON DIOXIDE SEQUESTRATION(12,7)\|EVAPORATOR CHAMBER(12,5)\|RETURN PIPELINE(12,5)\|ABSORBING AMMONIA(12,3)\|CARBONATED SILICATE SLURRY(12,1)\|CHILLED SLURRY(11,2)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|UNDERGROUND REACTOR(11,2)\|BLACK COAL MWE(10,1)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|INCOMING REACTANT PIPELINE(10,1)\|SILICATE SLURRY CIRCULATION(10,1)\|RAW FLUE GAS(9,6)\|FLUE GAS FILTER(9,5)\|REACTION SOLUTION(9,5)\|CARBONATION REACTION(9,2)\|EVAPORATOR VESSEL(9,2)\|FIRED ELECTRICITY GENERATION PLANT(9,2)\|AMMONIA TONNE(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|INCOMING SILICATE SLURRY(9,1)\|MAXIMIZE REGENERATION(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OVERLAND PIPELINE(9,1)\|REACTED SLURRY RISING(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|STACKED SUBCHAMBER(9,1)\|ABSORBER AQ(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HOT PRESSURIZED FMAL PRODUCT(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|RAW REACTIVE SLURRY(8,1)\|TONNE AMMONIA(8,1)\|POWER STATION SITE(7,7)\|CARBON DIOXIDE TONNE(7,2)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|SLURRY FEED(7,2)\|CONDENSATION(6,3)\|CENT CARBON DIOXIDE(6,2)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA CONCENTRATION(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(6,1)\|CARBONATE MINERAL FINAL EMPLACEMENT(6,1)\|CONCENTRIC PIPE(6,1)\|FINAL PERMANENT REPOSITORY(6,1)\|GAS REMNANT(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INORGANIC COMPONENT(6,1)\|INSOLUBLE CARBONATE NATURE(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|NATURAL SILICATE(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRETREATMENT EXTENT(6,1)\|PYROXENE RICH MINERAL(6,1)\|PYROXENE SILICATE METAL(6,1)\|RAW SLURRY(6,1)\|REACTED SLURRY RISE(6,1)\|RESIDUAL VAPOR(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE CONVERSION(6,1)\|SLURRY REACTION(6,1)\|TRANSPORTING ORE(6,1)\|FINAL PRODUCT SLURRY(5,4)\|ADJACENT FLOW PATH(5,2)\|BOTTOM ASH PULVERIZATION(5,2)\|CHILLED AMMONIA WATER(5,2)\|LIMESTONE(5,2)\|RESIDUAL AMMONIA SCRUBBER DETAIL(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|AMMONIA VAPOR FLOW(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|HOT PRODUCT PIPELINE(5,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(5,1)\|KEEPING UP(5,1)\|LIQUID PRESSURIZATION(5,1)\|MAGNESIUM CARBONATE EXTRACTION(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|OXIDE REACTION(5,1)\|PERFOI RING(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|WT SLURRY(5,1)\|AMMONIUM SALT(4,4)\|REACTION CHAMBER(4,4)\|SOX(4,3)\|INSULATION(4,2)\|LIQUID AMMONIA RECOVERY(4,2)\|SHELL(4,2)\|SINGLE INTEGRATED(4,2)\|AIR PREHEATING(4,1)\|AMMONIA ABSORBER(4,1)\|AMMONIA GAS PIPE DIAMETER(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIUM CARBONATE COMPOUND(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CARBON DIOXIDE ABSORPTION ZONE(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|GAS LIQUID SEPARATOR(4,1)\|GEOLOGICAL CONDITION PERMIT(4,1)\|HARMFUL CARBON DIOXIDE GAS(4,1)\|HEAT BALANCE FIGURE(4,1)\|HEAT CONSERVATION(4,1)\|ID MOL(4,1)\|INDICATIVE MASS(4,1)\|LATTER CONTINUING(4,1)\|LIDDELL POWER STATION(4,1)\|\|(AU2009250983)\|METAL SILICATE SLURRY(100,36)\|REACTION SLURRY(83,26)\|METAL SILICATE(82,44)\|LIMESTONE PULVERIZATION(65,1)\|MAGNESIUM RICH SILICATE(62,9)\|METAL CARBONATE(58,14)\|AMMONIATED SLURRY(58,5)\|AMMONIA(48,71)\|PERMANENT SEQUESTRATION(45,2)\|CARBON DIOXIDE(43,69)\|REACTOR(43,26)\|EVAPORATOR(43,8)\|REACTION ENHANCEMENT(42,6)\|SEQUESTERING CARBON DIOXIDE(42,3)\|COAL FUEL(42,1)\|PIPELINE(41,28)\|GAS STREAM(40,12)\|SLURRY(39,45)\|METAL SILICATE ROCK(37,3)\|AMMONIA ABSORPTION RECOVERY VESSEL(37,1)\|SCRUBBING CHAMBER(36,18)\|FLOW PATH(35,12)\|RECOVERING AMMONIA(33,8)\|AMMONIA ABSORPTION CHAMBER(33,7)\|NATURALLY OCCURRING SINK(33,1)\|LIQUID PRESSURIZATION(30,2)\|AMMONIA WATER(29,15)\|INSOLUBLE CARBONATE(28,4)\|RETURN PATHWAY(28,2)\|POWER THIRSTY CLIMATE(28,1)\|DOLOMITE(27,4)\|CHILLED SLURRY(27,3)\|AMMONIA ABSORPTION CHILLER(25,2)\|CARBON SEQUESTRATION(24,9)\|PYROXENE SILICATE METAL(23,2)\|REACTOR CONTROL(23,1)\|POWER STATION BOILER(22,1)\|CARBON DIOXIDE SEQUESTRATION(19,24)\|OLIVINE(19,7)\|EVAPORATOR CHAMBER(19,6)\|AMMONIA ABSORPTION(18,2)\|CARBON DIOXIDE REMOVAL(18,2)\|SEQUESTER CARBON DIOXIDE(18,2)\|CARBON SEQUESTRATION(17,3)\|DUTY(17,2)\|AMMONIA RECOVERY VESSEL(16,14)\|UNDERGROUND CHAMBER(16,9)\|PRESSURIZED LIQUID AMMONIA(15,3)\|OVERLAND AMMONIA PIPELINE(15,2)\|RECIRCULATION(15,2)\|CARBON DIOXIDE SEQUESTRATION(14,8)\|CHILLED AMMONIA WATER(14,3)\|ABSORPTION(14,2)\|CARBON CAPTURE(14,1)\|LAGGED ABOVEGROUND PIPELINE(14,1)\|FLY ASH(12,7)\|POWER STATION FLY ASH(12,4)\|CHAMBER PRODUCT(12,2)\|ABSORBENT SLURRY DELUGING SPRAY(12,1)\|POWER STATION(11,26)\|AMMONIUM SALT(11,5)\|MINERAL CARBONATION(11,3)\|PRODUCING CHAMBER(11,2)\|ABSORBING AMMONIA(10,3)\|HUNTER VALLEY(10,2)\|TARGET METAL(10,2)\|RETURN PIPELINE(9,5)\|HOT SILICATE SLURRY(9,2)\|INCOMING REACTIVE SLURRY(9,2)\|TONNE CO2 GWH(9,2)\|UNDERGROUND REACTOR(9,2)\|CARBONATED SILICATE SLURRY(9,1)\|RAW FLUE GAS(8,6)\|BLACK COAL MWE(8,1)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|MAFIC ROCK(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|FLUE GAS FILTER(7,5)\|REACTION SOLUTION(7,5)\|CARBONATION REACTION(7,2)\|CO2 ABSORBER(7,2)\|EVAPORATOR VESSEL(7,2)\|FIRED ELECTRICITY GENERATION PLANT(7,2)\|AMMONIA TONNE(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|MAXIMIZE REGENERATION(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|STACKED SUBCHAMBER(7,1)\|ULTRAMANE ROCK(7,1)\|CARBON DIOXIDE TONNE(6,2)\|MINERAL MATTER(6,2)\|PUMPING ENERGY(6,2)\|SLURRY FEED(6,2)\|ABSORBER AQ(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|ID MON CO2(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|RAW REACTIVE SLURRY(6,1)\|TONNE AMMONIA(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|CENT CARBON DIOXIDE(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA CONCENTRATION(5,1)\|AMMONIA SLIP(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(5,1)\|CARBONATE MINERAL FINAL EMPLACEMENT(5,1)\|CONCENTRIC PIPE(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|INSOLUBLE CARBONATE NATURE(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|MORL CO2(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,4)\|ADJACENT FLOW PATH(4,2)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|RESIDUAL AMMONIA SCRUBBER DETAIL(4,2)\|WOLLASTONITE(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|AMMONIA VAPOR FLOW(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENT NITROGEN(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(4,1)\|KEEPING UP(4,1)\|MAGNESIUM CARBONATE EXTRACTION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|WT SLURRY(4,1)\|REACTION CHAMBER(3,4)\|SOX(3,3)\|INSULATION(3,2)\|LIQUID AMMONIA RECOVERY(3,2)\|SHELL(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA GAS PIPE DIAMETER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIUM CARBONATE COMPOUND(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BICARBONATE(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CARBON DIOXIDE ABSORPTION ZONE(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|GAS LIQUID SEPARATOR(3,1)\|GEOLOGICAL CONDITION PERMIT(3,1)\|HARMFUL CARBON DIOXIDE GAS(3,1)\|HEAT BALANCE FIGURE(3,1)\|HEAT CONSERVATION(3,1)\|INDICATIVE MASS(3,1)\|	(EP2134449)\|1. A carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor (52,70) that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|2. A process in accordance with claim 1, wherein in step (i), pressurised liquid ammonia is charged into the metal silicate slurry in such a manner that the liquid ammonia partially flashes to a vapour to produce the ammonia/water/metal silicate slurry.\|3. A process in accordance with claim 1 or claim 2, wherein the step of scrubbing the gas stream comprises exposing the carbon dioxide-containing gas stream into a spray of the slurry.\|4. A process in accordance with any one of the preceding claims, wherein the step of controlling the reactor comprises elevating at least one of a pressure and temperature of the reactor (52, 70) so as to enhance the reaction between the carbon dioxide and the metal silicate.\|5. A process in accordance with any one of the preceding claims, wherein the reactor (52,70) is a pipeline (52) comprising multiple flow paths such that the reaction takes place along the length of one of the flow paths while another of the flow paths is utilised to supply the metal silicate slurry to the first stage; optionally comprising the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\|6. A process in accordance with any one of claims 1 to 4, wherein the reactor is an underground chamber (70) located at a depth that provides sufficient pressure to enhance the reaction between the carbon dioxide and the metal silicate.\|7. A process in accordance with any one of the preceding claims, comprising the further step of recovering ammonia resulting from the reaction stage (iii) and recycling it to the first stage; optionally comprising the further step of introducing an alkali to the metal carbonate product resulting from the reaction stage (iii) prior to carrying out the ammonia recovery step.\|8. A process in accordance with claim 7, wherein the ammonia is recovered as both a liquid and a gas, with the liquid being converted partially to a vapour for recycling in the first stage and the gas being extracted, condensed and mixed with the metal silicate before it is supplied in the first stage; optionally wherein the step of recovering the ammonia is effected in a recovery vessel (54) which is pressurised to facilitate the recovery of ammonia in liquid form.\|9. A process in accordance with any one of the preceding claims, comprising the further step of grinding a metal silicate rock to produce the metal silicate slurry.\|10. A process in accordance with any one of the preceding claims, wherein the metal silicate is a magnesium silicate.\|11. A process in accordance with any one of the preceding claims, wherein the slurry of metal silicate rock is chilled prior to passing the slurry to the second stage.\|12. A process in accordance with any one of the preceding claims, wherein:\| - prior to passing the ammonia to the first stage, a pressurised liquid ammonia is allowed to expand in an evaporator stage so as to provide a cooling effect in the evaporator stage; and\| - the resultant ammonia/water/metal silicate slurry produced in the first stage is passed through the evaporator stage so as to chill the ammonia/water/metal silicate slurry.\|13. A process in accordance with claim 12, comprising the further step of withdrawing the chilled slurry and passing it to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammonia/water/metal silicate slurry to thereby absorb the carbon dioxide into the slurry.\|14. A process in accordance with claim 13, comprising the further step of recirculating the reactive slurry containing absorbed carbon dioxide through the evaporator stage and then to the scrubbing stage.\|15. A process in accordance with any one of claims 12 to 14, wherein the evaporator stage is carried out in an evaporation chamber (82).\|16. A system for (10) sequestering carbon dioxide from a gas stream, the system for comprising:\| (a) a first apparatus (28,30) for removing the carbon dioxide from the gas stream and for absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and\| (b) a reactor (52,70) for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|17. A system in accordance with claim 16, wherein the first apparatus comprises an ammonia absorption chiller (82) arranged to mix the metal silicate with ammonia to produce the ammoniated slurry.\|18. A system in accordance with claim 16 or claim 17, wherein\| (a) the reactor is a pipeline (52) comprising multiple flow paths and wherein the reaction takes place along the length of one of the flow paths; or\| (b) the reactor is a chamber (70), located in use underground; optionally wherein the chamber is located at a depth that provides sufficient pressure to enhance the reaction between the carbon dioxide and the metal silicate.\|19. A system in accordance with claim 18, wherein:\| - in the case of (a) the pipeline (52) comprises:\| a first flow path that (44) carries the metal silicate slurry to the first apparatus (28,30); and\| a second flow path (52) that carries from the first apparatus (28,30) the reactive slurry comprising carbon dioxide absorbed in an ammonia/water/metal silicate slurry, the second flow path being controlled so as to encourage the carbon dioxide to react with the metal silicate and produce a metal carbonate;- in the case of (b) the reactive slurry that comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry is provided to the chamber (70) for a sufficient period to enable it to react.\|20. A system in accordance with any one of claims 16 to 19, wherein the metal silicate comprises a magnesium silicate.\|21. A system in accordance with any one of claims 16 to 20, further comprising an ammonia absorption recovery vessel arranged to recover ammonia contained in the metal carbonate product.	(EP2134449)\|Technical Field\|[0001] This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|Background to the Invention\|[0002] There is increased focus on reducing carbon dioxide emissions to the atmosphere, to help minimise the effects of global warming. Carbon dioxide sinks exist naturally, with the main naturally occurring sink being the ocean. Plants are also an effective form of carbon dioxide sink and use photosynthesis to remove carbon from the atmosphere by incorporating it into biomass. However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\|[0003] The major source of harmful carbon dioxide gases are large fossil fuel power stations which, when fuelled by black coal, on average typically output around 0.8 to one tonne of the gas for each MegaWatt-hour (MWh) of electricity they generate. For example, a large power station such as the 2,640 MW Bayswater in the Hunter Valley of New South Wales, Australia, in generating 20 million MWh of electricity in a year, would also output 18 million tonnes of carbon dioxide. It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations. It would also be advantageous if a system and method were provided for the disposition of the gas to be independently audited.\|[0004] Known methods of sequestering carbon dioxide are described in WO 2006/008242, WO 200=4/0940=t3, WO 2005/108297 and WO 200=4/0987=40. WO 2006/022885 describes a method of ultra-cleaning a combustion gas, followed by capture and regeneration of carbon dioxide. The application does not describe a process in which a reaction between a metal silicate is controlled to produce a metal carbonate. There is also no disclosure of absorbing carbon dioxide in an ammoniated slurry that contains a metal silicate dispersed through it.\|Summary of the Invention\|[0005] In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|[0006] It should be noted that the terminology "gas stream containing carbon dioxide" does not mean that the stream contains only carbon dioxide, and may contain other off gases.\|[0007] In an embodiment of step (i), pressurised liquid ammonia is charged into the metal silicate slurry in such a manner that the liquid ammonia partially flashes to a vapour to produce the ammonia/metal silicate slurry.\|[0008] An embodiment of step (ii) may comprise exposing the carbon dioxide-containing gas stream to a spray of the slurry.\|[0009] An embodiment of step (iii) may comprise elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\|[0010] In an embodiment, the reactor is a pipeline. The pipeline preferably comprises multiple flow paths. In an embodiment, the reaction takes place along the length of one of the flow paths. Another of the flow paths may be utilised to supply the metal silicate slurry to the first stage.\|[0011] In an embodiment, the method comprises the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\|[0012] In an embodiment, the reactor is a chamber located in use underground. Preferably, the chamber is located at a depth that provides sufficient pressure to enhance the reaction between the carbon dioxide and the metal silicate. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0013] In an embodiment, the method may also comprise the step of recovering ammonia resulting from the reaction stage (iii) and recycling it to the first stage. In an embodiment, an alkali is added to the final product prior to performing the step of recovering ammonia. The alkali may be power station fly ash or pulverised bottom ash obtained by filtering or otherwise cleaning the carbon dioxide-containing flue gas stream. The ammonia may be recovered as both a liquid and a gas, with the liquid being converted partially to a vapour for recycling in the first stage and the gas being extracted, condensed and mixed with the metal silicate before it is supplied in the first stage.\|[0014] In an embodiment, the step of recovering the ammonia is effected in a recovery vessel which is pressurised to facilitate the recovery of ammonia in liquid form at ambient temperatures. In an embodiment, the recovery vessel is in use located at a depth sufficient for achieving the pressure to recover the ammonia in liquid form. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0015] In an embodiment the process comprises the further step of grinding a metal silicate rock to produce the metal silicate slurry. The metal silicate slurry may comprise 30 to 60% finely ground solids by weight. In an embodiment, the metal silicate is a magnesium-rich silicate mineral. The magnesium rich silicate may be comprised of a serpentine- and/or olivine- and/or pyroxene-rich mineral.\|[0016] In accordance with a second aspect, the present invention provides a system for sequestering carbon dioxide from a gas stream, the system comprising:\| (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and\| (b) a reactor for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|[0017] In an embodiment, the first apparatus comprises an ammonia absorption chiller arranged to (a) chill the metal silicate slurry and (b) mix the chilled slurry with ammonia to produce the ammoniated slurry. In an embodiment step (a) is carried out prior to step (b).\|[0018] The reactor may comprise the pipeline as set forth in the first aspect. In an alternative embodiment, the reactor may comprise the chamber as set forth in the first aspect. The metal silicate may comprise a magnesium rich silicate as set forth in the first aspect. In an embodiment, the system comprises a recovery vessel arranged to recover ammonia contained in the metal carbonate product.\|[0019] In accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the carbon dioxide to react with the metal silicate and produce a metal carbonate.\|[0020] In accordance with a fourth aspect of the present invention there is provided a method for causing a slurry, comprising carbon dioxide absorbed in an ammonia/water/metal silicate slurry, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the carbon dioxide and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|[0021] In an embodiment, the slurry provided to the chamber is the reactive slurry produced in the process as set forth in the first aspect. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0022] In an embodiment, the method comprises the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber. In an embodiment, the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.\|[0023] In accordance with a fifth aspect there is provided a power station utilising a carbon sequestration system in accordance with the second aspect, the system arranged to sequester carbon dioxide from flue gas emitted by the power station.\|[0024] In accordance with a sixth aspect, in an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, there is provided the steps of: (i) prior to passing ammonia to the absorption process, allowing the ammonia in pressurised liquid form to expand in an evaporator stage so as to provide a cooling effect in that stage; and (ii) passing the water/metal silicate slurry through the evaporator stage so as to chill said water/metal silicate slurry, prior to mixing it with the ammonia in the ammonia absorber process.\|[0025] In an embodiment, the process comprises the further step of providing the ammoniated slurry to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammonia/water/metal silicate slurry to thereby absorb the carbon dioxide into a reactive slurry.\|[0026] In an embodiment, the process comprises the further step of passing reactive slurry which is to be re-circulated through the scrubbing chamber through the evaporator stage prior to re-circulation. The evaporator stage may be implemented in an evaporator chamber. The scrubbing stage may be implemented in the first apparatus, as set forth in the second aspect.\|[0027] In accordance with a seventh aspect of the present invention there is provided an ammonia absorption chamber arranged to implement the process as set forth in the sixth aspect.\|[0028] In accordance with an eighth aspect of the present invention there is provided a method of extracting a target metal from a metal silicate comprising the step of mixing the metal silicate with a solution that comprises ammonia and ammonium salt, whereby the ammonia reacts with the metal silicate to cause the target metal to dissolve into the solution.\|[0029] In an embodiment the method comprises the further step of grinding the metal silicate and forming it into a slurry prior to mixing the metal silicate with the solution.\|[0030] In an embodiment the mixing takes place in an ammonia absorption chamber.\|[0031] In an embodiment the metal silicate is a magnesium-rich silicate.\|[0032] In an embodiment the magnesium-rich silicate is a serpentine and/or olivine and/or pyroxene silicate metal.\|[0033] In an embodiment the ammonium in solution comprises ammonium carbonate.\|[0034] In an embodiment the target metal dissolves into the solution and then precipitates as a metal carbonate to be removed for recovery.\|[0035] In an embodiment the target metal is one or more of magnesium, iron, copper and nickel. The dominant metal within the metal silicate may comprise magnesium.\|[0036] In a ninth aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a chilled slurry of a metal silicate rock with ammonia so as to produce a chilled ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the chilled solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|Brief Description of the Drawings\|[0037] An embodiment of the present invention will now be described, by way of example only, with reference to the accompanying drawings, in which:\| Fig. 1 is a schematic of a carbon dioxide sequestration system according to an embodiment of the present invention;\| Fig. 1A is a further schematic of a carbon dioxide sequestration system according to an embodiment of the present invention with additional detail of the Residual Ammonia scrubber, Ammonia absorber, and CO2 absorber shown.\| Fig. 2 is a process flow diagram showing a method of sequestering carbon dioxide using the system of Fig. 1, in accordance with an embodiment of the present invention;\| Fig. 3 is a schematic of a pressure exchange apparatus utilised by the carbon dioxide sequestration system of Fig. 1, in accordance with an embodiment of the present invention;\| Fig. 4 is a schematic of a heat exchange apparatus utilised by the carbon dioxide sequestration system of Fig. 1, in accordance with an embodiment of the present invention; and\| Fig. 5 is a schematic of a carbon dioxide sequestration system, according to an alternative embodiment of the present invention.\| Fig. 5A is a further schematic of a carbon dioxide sequestration system, according to an alternative embodiment of the present invention with additional detail of the Residual Ammonia scrubber, Ammonia absorber, and CO2 absorber shown.\|Detailed Description of an Embodiment\|[0038] In the following description, an embodiment of the present invention is described in the context of a system, apparatus and method for the capture and sequestration of carbon dioxide contained within flue gases emitted by a fossil fuel-fired power station. However, it is to be understood that the system, apparatus and method could equally be utilised for the permanent sequestration of carbon dioxide from any source and is not limited to the particular arrangement described herein.\|[0039] With reference to Fig. 1 there is shown a flow diagram of a system 10 for performing a carbon dioxide (CO2) sequestration process from a gas feed stream containing carbon dioxide outputted from a power station, in accordance with an embodiment of the present invention. With additional reference to Fig. 2, the system is arranged to perform the process 100 of (i) in a first stage, mixing a slurry of chilled ground metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the ammonia/water/metal silicate solution to thereby absorb the carbon dioxide into a reactive solution; and (iii) passing the reactive solution through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate and by-product silica (stage three).\|[0040] In an embodiment, the slurry of ground metal silicate rock is chilled by circulating the slurry through a vessel in which ammonia evaporates. In an embodiment another stage is carried out prior to stage (ii), namely contacting flue gases in a vessel in a counter-current, staged manner so that residual ammonia in the flue gases is scrubbed from these gases to levels low enough to allow their final discharge in the atmosphere.\|[0041] In the illustrated embodiment the three stages are performed successively, with the first two stages occurring within a first apparatus 20 in the form of two separate reaction chambers, namely an absorption chamber 28 and a scrubbing chamber 30, and the last stage occurring within a reactor in the form of a pipeline 52 which may, for example, connect the mine site to the power plant. As will be described in detail in subsequent paragraphs of the specification, the reactor may alternatively take the form of an underground chamber (see Fig. 5) excavated at a sufficient depth to facilitate the conditions for the carbonation reactions to take place.\|[0042] The carbon dioxide sequestration process utilised in embodiments of the present invention is based on mineral carbonation. Mineral carbonation is a reaction between a metal-oxide bearing material and carbon dioxide. The metal-oxide bearing material may for example be alkaline-earth metals. Advantageously, the process 100 does not require the source of carbon dioxide to be particularly pure. In mineral carbonation, carbon dioxide reacts with the metal oxide bearing material to generate insoluble carbonates, that is to say:\| MO + CO2 → MCO3 + heat (1)\|which is an exothermic reaction, occurring more rapidly at elevated temperature, typically above 200°C. Certain chemicals may serve to increase the rate at which this reaction proceeds without being consumed themselves, i.e. they serve as catalysts. The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|[0043] The exact nature of the insoluble carbonates formed by the reaction depends on the metal-oxide bearing material. Suitable materials may be naturally occurring alkaline-earth metal-rich silicate rocks which contain mineral constituents such as serpentinite (Mg3Si2O5(OH)4), olivine (Mg2SiO4), orthopyroxene (MgSiO3), talc (Mg3Si4O10(OH)2) and wollastonite (CaSiO3). In practice, the element Iron (Fe) may substitute for some of the Magnesium (Mg) or Calcium (Ca). Other suitable materials include alkaline industry residues such as slag from steel production, the ash (both fly and bottom) from pulverised coal-fired boilers, the ash remaining from the combustion of paper recycling residues (de-inking ash), and cement. The amount of heat generated in the reaction will depend on the specific metal and on the mineral containing the metal oxide as can be seen below in the case of three natural silicates (heat values are given per unit mole of CO2 and at standard conditions (25°C and 0.1 MPa):\| Olivine\| Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 + 89 kJ mol-1 CO2 (2a)\| Serpentine\| Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol-1 CO2 (2b)\| Wollastonite\| CaSiO3 + CO2 → CaCO3 + SiO2 + 90 kJ mol-1 CO2 (2c)\|[0044] A preferred silicate rock (because of its greater abundance in continental land masses) comprises the mineral serpentine, Mg3Si2O5(OH)4, All of these minerals may be pre-treated to increase the surface area of rock that can come into direct contact with the carbon dioxide. In an embodiment, the pre-treatment involves crushing, grinding and/or milling of the mineral, as well as some mechanical classification and separation. Typically, these minerals would be wet-milled in ball mills or equivalent to form a finely ground metal silicate slurry (hereafter 'silicate slurry') 36 wherein 90% of the mineral matter was finer than 40 microns. However, the extent of the pre-treatment is dependent upon the source and type of mineral(s) being used in the process.\|[0045] With specific reference to Fig. 1, the carbon dioxide sequestration system 10 will now be described in detail. The system 10 receives a raw flue gas mixture feed stream 32 that has been generated and subsequently emitted by a power station (not shown). In the embodiment described herein, the raw flue gas mixture 32 is passed though a filter 34 to remove particulate matter. Suitable filters may include fabric filters, electrostatic precipitators and the like. Cleaning the raw flue gas mixture 32 serves to minimise both the maintenance costs in downstream gas-handling equipment and the concentrations of particulates in flue gases ultimately discharged to the atmosphere. It will be understood, however, that while desirable for process reasons, it is not essential that the raw flue gas mixture 32 be cleaned of particulates before it enters the scrubbing chamber 30.\|[0046] To maximise heat recovery in the system 10, the filtered flue gas mixture is then passed through a heat exchange apparatus in the form of a heat exchanger 34 so that the sensible heat of the filtered flue gas mixture (typically emitted at a temperature of around 135°C) is exchanged with the cooler gasses being expelled from the scrubbing chamber 30 of the first apparatus 20 and the filtered flue gas mixture is cooled to its water-vapour saturation temperature (i.e. to about 50°C). Suitable heat exchangers may include, for example, recuperative-type heat exchangers, such as the Ljungstrom rotary design as used for air pre-heating in power stations.\|[0047] As mentioned in preceding paragraphs, the carbon dioxide sequestration system 10 receives a source of silicate slurry 36. According to the embodiment described herein, the silicate slurry source is located near or at the mine site from which the silicate rocks are sourced. As previously described, the silicate mineral sourced from the mine site is finely ground (preferably by wet-milling in ball mills or equivalent to form the slurry) wherein 90% of the mineral matter is finer than 40 microns. The silicate slurry 36 is subsequently passed through a first pressure-exchange apparatus 38. To minimise power consumption, the pressure of the silicate slurry 36 may be increased by exchanging pressure with the final metal carbonate/silica product (hereafter `final product'), typically to a pressure of approximately 10 Bar. In addition, to minimize heat losses from the system 10 (and to ensure that the final product is cooled to a suitable temperature before it is emplaced in its final permanent repository), the silicate slurry 36 passes counter-currently through a second heat exchanger 40 to absorb the surplus sensible heat contained in the final product. At a second pressure-exchange apparatus 42, the pressure of the silicate slurry 36 is further increased, this time to a substantially higher level (typically 100 Bar). Again, this boost in pressure is achieved by exchanging pressure, but this time with the carbonate/silica slurry prior to it undergoing treatment in the ammonia gas recovery vessel 54 (as will be described in detail in subsequent paragraphs).\|[0048] A pipeline 44 connects the first apparatus 20 to the mine site and is used to transport the silicate slurry 36 used in the sequestration process 100. As will be described in more detail in subsequent paragraphs, an alternate path 52 in the pipeline 44, in this embodiment, also serves to act as a controlled reactor in which the metal carbonate reaction largely takes place. At or near to the power station site, the silicate slurry 36 is passed counter-currently through a third heat exchanger 46 and a third pressure-exchange apparatus 48, where the silicate slurry 36 is cooled and reduced in pressure by exchange with the reactive slurry discharged from the first apparatus 20, before being fed directly into the evaporator vessel 82, where ammonia which has passed through the expansion valve 29 and is now at a very low temperature, cools the silicate slurry to near freezing. To ensure that the silicate slurry 36 is not actually frozen, a portion of this slurry is circulated through the evaporator vessel. The chilled silicate slurry passes downwards through a vessel, the residual ammonia scrubber, in such a way that cleaned and cooled flue gases that have been stripped of most of their carbon dioxide content, pass upwards from below. There may be as many as six counter-current contacting stages, such that the cleaned, largely carbon dioxide-free flue gases may leave the system with less than one part per million of ammonia.\|[0049] The silicate slurry, now charged with any ammonia arriving in flue gases from below, enters the ammonia absorber 28, where it absorbs into solution all of the ammonia that is recovered in the ammonia recovery vessel 54 so as to produce a ammonia/water/metal silicate slurry.\|[0050] The ammonia is recycled from the ammonia gas recovery stage of the process (described in subsequent paragraphs), with additional quantities required only to make up for losses, which should be small. Recovered liquid ammonia (which may contain small amounts of water) is supplied to the absorption chamber 28 by way of a pipeline 60, under pressure. In a preferred embodiment, pressurised liquid ammonia passes through the pressure reduction valve 29, which reduces its pressure to near atmospheric, at which pressure it discharges into a vessel, the evaporator chamber 82, prior to entering the absorption chamber 28. A portion of the ammonia will flash to vapour upon entering the evaporator chamber 82. The ammonia, in vaporising, absorbs substantial quantities of latent heat which is withdrawn from the slurries circulating through banks of tubes in the evaporator chamber 82, thereby chilling them to near freezing. In the embodiment shown in Fig. 1, the heat absorbed as the ammonia vaporises is drawn from the silicate slurry used as the residual carbon dioxide scrubbing medium in the residual ammonia scrubbing chamber. This is to ensure that the scrubbing medium last in contact with the cooled, filtered flue gases is the most chilled.\|[0051] The vaporised ammonia flows from the evaporator chamber 82 directly into the ammonia absorption chamber 28, wherein it is rapidly absorbed into the deluging spray of circulating silicate slurry 36 after this has passed downwards through the several stages of the residual carbon dioxide scrubber, to produce the ammonia/water/metal slurry used as the circulating scrubbing medium for the carbon dioxide scrubbing chamber 30. When the ammonia is absorbed in the silicate slurry 36 a substantial quantity of heat is liberated: the heat of solution of ammonia gas in water. Much of this heat is removed as the slurry circulates through the heat exchanger 84. As illustrated, the heat exchanger 84 and cooling tower also serve to remove much of the excess low-grade heat generated from the absorption of the ammonia in the silicate slurry.\|[0052] The cooled filtered flue gas mixture passing through the heat exchanger 34 enters the scrubbing chamber 30 where the gas mixture passes upwards through deluging sprays of absorbent slurry, the absorbent slurry having been drawn from the ammonia absorption chamber 28 and discharged into the head space of the scrubbing chamber 30. When carbon dioxide is absorbed in the ammonia/water/metal silicate slurry, a further substantial quantity of heat is liberated, as carbon dioxide and ammonia form in solution a series of ammonium carbonate compounds. With sufficient ammonia supplied to the absorption chamber 28 to achieve 90 per cent capture of carbon dioxide, the tendency will be to form the bicarbonate NH4HCO3 in preference to the normal carbonate (NH4)2CO3 and the carbamate, NH2COONH4, which will also be present in smaller quantities, perhaps along with some urea, CO(NHZ)2. The system 10 is configured such that the coldest slurry will be the last to contact the stripped (of carbon dioxide) flue gas mixture, in such a way that ammonia slip (losses in final flue gases to the atmosphere) are essentially eliminated. In the embodiment shown in Fig. 1, the scrubbing chamber 30 is shown as being constructed separately to the absorption chamber 28. Suitable scrubbing chambers may be generally similar to the type used for flue gas desulphurisation.\|[0053] As previously described, the sensible heat is removed from the filtered flue gas mixture in the first heat exchanger 34, cooling it to around 50°C, before entering the scrubbing chamber 30. The clean flue gases exiting the scrubbing chamber 30 typically comprise around 95 per cent nitrogen and inerts by volume. The balance comprises some oxygen and around 1.5 per cent carbon dioxide, being the remnant quantity of this gas after some 90 per cent had been stripped out in the scrubbing chamber 30.\|[0054] The resultant product of this two-stage process is a reactive solution in the form of a metal silicate slurry in an aqueous phase that is itself primarily a solution of ammonium carbonates. A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor. On route to the mine site, at or near to the power station, the reactive slurry is pressurised at the third pressure-exchange apparatus 48 to a high pressure of around 120 Bar (above the critical pressure of ammonia) and also heated to close to the boiling point of water at the pressure in question. Heating is accomplished firstly by transferring heat from the incoming silicate slurry arriving from the mine at the heat exchanger 46, and also by injection of steam 54. Without being bound by theory, the inventor anticipates that, subject to the process design assumptions of Example 1 (see table below), around 600 tonnes per hour of steam would be required to raise the temperature of the reactive slurry by around 100°C, to say 225°C, at which temperature the carbonation reactions are likely to reach acceptable rates. Heat liberated from the reaction between carbon dioxide and the metal silicate in the reactive slurry, which is highly exothermic, is capable on its own of raising the reactive slurry temperature by around 75°C (under the assumptions made in respect of Example 1), to yield a final temperature of some 300°C by the time the reactive slurry reaches the vicinity of the mine site, or site of other final emplacement. This temperature rise would be obtained despite some losses along the length of the return pipeline 52, notwithstanding attempts to minimise such losses by cladding this pipeline 52 throughout its length by suitable insulation (lagging).\|[0055] In the return pipeline 52 of the pipe reactor, most if not all of the carbon dioxide present in the reactive slurry can react with the silicate minerals and convert to insoluble carbonate during approximately the few first hours of transit. Each hour may correspond to a 10 kilometre length of this pipeline. In practice, however, the power station and the mine site may be much more than this distance apart, thereby allowing more than adequate time for reactions to proceed essentially to completion resulting in the metal carbonate product that contained most if not all of the carbon dioxide originally scrubbed from the power station flue gases. A high concentration of ammonia is maintained in the slurry throughout its passage from the power station to the mine/quarry or other emplacement site.\|[0056] When the final product in the return pipeline 52 reaches the vicinity of the mine site, as described above, it is passed through the second pressure-exchange apparatus 42 to lower the pressure of the stream from perhaps as high as 120 Bar to around 15-20 Bar, before entering the ammonia gas recovery vessel 54. With the temperatures indicated on Fig. 1, all of the ammonia and some of the water flash to vapours (the water would boil, the ammonia being driven out of solution) as the final product enters the ammonia gas recovery vessel 54, a consequence of a drop in temperature of more than 100°C. As shown in Fig 1, the hot pressurised final product transfers its sensible heat to the contents of the ammonia gas recovery vessel 54. This heat input assists to maximise the system's efficiency, as stripping the ammonia from the product as a gas absorbs considerable heat energy. To minimize the waste products generated by the system 10, and prior to entering the pipeline 44 for delivery to the continuous reactor 22, silicate slurry from the mine site is fed and re-circulated in the residual ammonia absorber 56 where residual vapours from the ammonia gas recovery vessel 54 are passed. A gas phase stream exiting from the top of the ammonia gas recovery vessel 54 contains essentially all of the free ammonia, which along with some water vapour condenses out in a condenser 58 to form a liquid phase that is mostly ammonia. In an embodiment, the condenser 58 is cooled by circulating water from dry (e.g. radiator-type) cooling towers, fin fan coolers, or, because no fans are required, a natural-draft cooling tower (not shown) such as used for cooling in the power station. This recovered liquid ammonia, representing the bulk of the ammonia injected into the circulating slurry in the absorption chamber 28, flows under pressure (aided by pumps, not shown) through an overland ammonia pipeline 60 to the power station site.\|[0057] The final product carbonate slurry (containing nearly all of the carbon dioxide in the original power station flue gases but now sequestered as carbonates), leaves the bottom of the ammonia gas recovery vessel 54. The final product slurry is free of ammonia, and in a form suitable for permanent emplacement in mine voids or other purpose-built repositories (not shown). In these emplacements the solids can settle and consolidate, releasing much of the aqueous phase as a clear supernatant. This supernatant may be collected and re-used in the process, for example, to prepare the silicate slurry 36 and returned to the power station site, via pipeline 44.\|[0058] It should be noted that not all of the ammonia added in the first apparatus 20 can be recovered and returned to the process via the overland ammonia pipeline 60. Some ammonia may end up as ammonium salts: sulphites and sulphates, and as ammonium nitrites and nitrates, from SOx and NOx respectively in the raw flue gases. If the raw flue gas source is a flue gas generated by a typical fossil fuel-fired power station, and assuming use of modern low-NOx burners, losses of ammonia via these reactions should will be minor. Their presence in the final carbonate product slurry may furthermore, assist with rehabilitation of the final emplacements of the carbonate minerals. Figure 1A illustrates an alternative embodiment including a residual ammonia scrubber positioned within the scrubbing chamber 30.\|[0059] It may be desirable to reduce the losses of ammonia that would occur in this way. In an embodiment, this is achieved by dosing, or otherwise adding to the reacted slurry immediately prior to its entry into the ammonia recovery vessel 58, an appropriate quantity of slaked lime or other suitable alkali. A source of such alkali may be power station fly ash or pulverised bottom ash. The presence of limestone or dolomite in the original coal may render them suitable for this duty; in passing through the boilers much of this limestone or dolomite will be converted to alkalis suitable for ammonia recovery: quicklime or dolime (dolomite-lime), respectively.\|[0060] Should it arise that the content of limestone or dolomite in the coal fuel is inadequate for the duty (as is likely to be the case with most power station fly ashes), it is possible to dose the appropriate quantity of pulverised limestone or dolomite to the power station boilers (not shown). This dosing may be conducted at a location in the hot combustion gas path where the gas temperatures are in the range 800-1,000°C, i.e. sufficient to convert these minerals to the reactive oxide forms (lime, or dolime respectively). For example, this may occur upstream of the boiler's economiser. When the ammonia-recovery vessel is close to the power station, as it would be in the case of the underground chamber reactor embodiment (Fig. 5), it may be appropriate to add all of the power station fly ash to the final product slurry to maximise the regeneration of ammonia for re-use in the process. In this manner, both fly ash and the final product slurry from the carbon sequestration process may be handled and co-disposed of as a single stream. An anticipated advantage stemming from the presence of fly ash having pozzolanic properties (a tendency to set in the presence of alkalis and moisture) in the final product, will assist with the rehabilitation process, by encouraging the final product/fly ash mix to "set".\|[0061] With reference to Fig. 3, there is shown an arrangement for the pressure-exchange apparatus described above. At the end of the reaction process, the pressure of the final carbonate-rich product must be reduced from approximately 120 Bar to atmospheric pressure. As described above, this is undertaken in two stages: from 120 Bar down to around 15 Bar, a pressure suitable for operation of the ammonia recovery stage, then from 15 Bar down to atmospheric pressure. Instead of merely reducing pressure by throttling valves, thereby losing the energy embodied in this pressure, the energy this pressure represents may be conserved by transferring it to the extent possible, in two stages, to the silicate slurry. In Fig. 3, slurry A comprises the products of the reactions that occur as the ammoniated, carbonated silicate slurry flow through the pipeline 44 from the power station to the mine site; while slurry B represents silicate slurry from the mine. A consequence of pressure exchange in these two stages is that slurry A's pressure would fall from around 120 Bar to near ambient pressure, while that of slurry B would rise: in the first stage (working from right to left) to around 10 Bar, then to perhaps 100 Bar in the second stage.\|[0062] Another pressure-exchange apparatus is also utilised at the power station site. Here, using the terminology of Fig. 3, slurry A represents the hot silicate slurry arriving via the pipeline from the mine; while slurry B comprises slurry exiting the scrubbing chamber 30 (i.e. silicate slurry now charged with ammonia and carbon dioxide, but at close to ambient pressures). A consequence of pressure exchange in this stage is that slurry A's pressure would fall from its arrival pressure (this may be 120 Bar, a pressure that would be maintained by booster pumping stations at strategic locations (not shown) along the pipeline 44 to overcome friction losses), to near ambient pressure. This pressure may be transferred (exchanged) to the extent possible to slurry B, thereby minimising the amount of pumping energy required to raise the pressure of this slurry to the levels required, here assumed to be 120 Bar. Since slurry A at this point will be at well below 120 Bar, pressure-exchange between slurries A and B alone may not be capable of raising the pressure of slurry B to 120 Bar. Also, the volume of slurry B may exceed that of slurry A. This is because of the much higher contents of carbon dioxide and ammonia, and of water condensed out of the power station flue gases. In an embodiment, additional pumping capacity may be installed to boost slurry B pressures to those required for the pipeline 44, and to pressurise those (relatively small) quantities of slurry B that cannot be pressurised by pressure-exchange with slurry A. For this function, conventional high-pressure diaphragm pumps, such as the Geho pump manufactured by Weir Netherlands b.v., may be implemented. This pumping, together with the pumping energy required to maintain pressures along the length of the pipelines, account for a substantial proportion of the total mechanical energy input to the total process. Other suitable pressure exchange/pump-turbine sets may comprise centrifugal pumps and radial-type hydraulic turbines. As the pressures are relatively high, the type of centrifugal pump may be a multi-stage barrel-type pump.\|[0063] With reference to Fig. 4 there is shown a configuration for the heat exchanger arrangements 40 & 46, according to an embodiment of the present invention. As previously discussed, high temperatures are required to initiate and accelerate the carbon sequestration reactions: the conversion of silicates to carbonates. These reactions, being exothermic, yield additional heat that can and should be applied to assist with creating the conditions needed for these reactions to proceed most efficiently. As shown, the heat exchanger arrangement is in the form of a simple shell-and-tube heat exchanger, consisting of two concentric pipes: the inner forms the "tube", the outer, the "shell". An advantage with this arrangement is that the heat exchanger can be made as long as is required to effect the desired transfer of heat: if necessary, many hundreds of metres long. For heat exchanger 40 (i.e. the heat exchanger on the mine site side), heat energy is transferred between the final carbonate/silica product (i.e. slurry A), which is hot, and the silicate slurry (slurry B), which is cool. For heat exchanger 46 (i.e. the heat exchanger on the power station side), slurry A would be hot silicate slurry from the mine, while slurry B would be slurry exiting the scrubbing chamber 30 (i.e. now charged with ammonia and carbon dioxide, but at close to ambient temperatures).\|[0064] Turning now to Fig. 5, there is shown an alternative system 200 for performing carbon dioxide sequestration which utilises (where geological conditions permit) an underground chamber as the reactor, as opposed to a pipeline reactor as illustrated in Fig. 1. In this embodiment, the reactor is in the form of a chamber 70 excavated from bedrock at a depth sufficient to allow the conditions for the core carbonation reactions to be generated entirely or partly by static head alone (e.g. 120 Bar for the carbonation reactions and 20 Bar for the recovery of ammonia gas from the reaction products). A chamber 70 excavated at a depth of approximately 1,000 meters and having a volume of 150,000 cubic meters, sufficient to allow for a 24 hours detention time for the contents, may be envisaged for holding the reactive slurry output from a system 200 fitted to an efficient 1,000MWe coal-fired power station. In practice a smaller chamber may suffice, should it arise that the reactions are essentially completed in less time.\|[0065] The silicate slurry 36 may be prepared either at the serpentine mine site and pumped overland to the power station site, or, the mineral could be railed, trucked or otherwise suitably transported to the power station site, and prepared there. Were the former course of action adopted, pipeline arrangements 44 would be considerably simpler than for the pipeline reactor embodiment described above with reference to Fig. 1. Specifically, the silicate slurry 36 would not be required to collect and transport heat and pressure energy from the mine site to the power station site, nor to host any residual ammonia. The pipeline 44 would simply be utilised for ore transport; whether it was transported as a lump product by rail or as slurry by pipeline would be determined mainly by economic considerations. It will be appreciated that in this embodiment, silicate slurry density could be substantially higher (e.g. 60 per cent solids), thereby reducing the volumes of silicate slurry required to be pumped, and allowing a lower pipeline velocity because of the reduced tendency for the solids in denser slurries to segregate and silt up the pipeline 44. Also, arrangements for conserving heat and pressure are much simpler than they would need to be for the pipeline reactor alternative.\|[0066] In Fig. 5, an injection pump 72 is utilised to drive the circulation of the reactive slurry from the scrubbing chamber 40, through a plurality of counter-current heat exchangers 74, 76, underground reactor 70 and ammonia gas recovery vessel 78 (flash/rectifying vessel) and back to the surface. It is envisaged that a formation of bubbles of ammonia gas may occur as the reacted slurry rises from the underground reactor 70 (a rise accompanied by a loss of static head, hence of pressure), thereby reducing the bulk density of the reacted slurry rising from the reactor. It follows that the required circulation could be achieved by entirely natural means: after the injection pump 72 has achieved the circulation necessary for the reaction to proceed, it may be taken off line. The design of injection pump 72 may be such that it could run backwards, that is to generate power, should the natural rate of circulation created by the buoyancy effect of ammonia bubbles forming in the reactor outlet pipe 80 be sufficiently strong.\|[0067] Heat exchangers 74, 76 are shown in schematic form at two locations on Fig. 5. In practice, the heat exchangers 74, 76 could be long, shell-and-tube designs, as shown in Fig. 4: they would span most of the vertical distance from the scrubbing chamber 40 down to the underground chamber 70. This is to say, whereas two separate pipelines are implied in Fig. 5, in practice, for most of their length they would be concentric: the annulus formed between the outer and concentric inner pipe would transport the hot reaction products, while the inner pipe would transport the products heading downward to the Reaction chamber. It will be understood by persons skilled in the art that this selection may be reversed.\|[0068] In contrast to the pipeline reactor configuration shown in Fig. 1, heating of the reactive slurry is accomplished by exchanging heat from the hot reaction products rising first from the ammonia gas recovery vessel 78, and as the raw slurry descended further, from hot slurry rising from the underground chamber 70. While some supplementary heat may be required, the heat generated by Equation 2(b) would be conserved, and available to heat raw reactive slurry.\|[0069] The design of the underground chamber 70 may be optimised to achieve some plug-flow characteristics. In an embodiment, the chamber 70 may have a high length-to-diameter ratio and be vertically aligned. In this manner, the incoming reactive slurry, being cooler hence slightly denser than the average contents of the reactive chamber 70, would tend to stratify at lower levels, displacing hotter slurry upwards. In an embodiment, the underground chamber 70 may be subdivided into two or more vertically stacked sub-chambers.\|[0070] There should be no requirement for separate agitation equipment in the reaction chamber to maintain the solids in suspension. As shown in Fig. 5, incoming reactive slurry enters the vessel close to its base, and it is envisaged that settling rates will be small relative to overall slurry up-flow rates. If, however, large residence times are required, implying in turn large reactor volumes, a form of agitation may be implemented.\|[0071] As will readily be appreciated, heat losses from the underground chamber 70 and pipelines may be much smaller than they would be even from a lagged above-ground pipeline and may be further reduced by insulation surrounding the reactor, pipelines and all other underground process vessels. Whereas an overland pipeline represents a plug-flow reactor, ideal conditions for a relatively slow series of reactions as are involved in carbon sequestration are also obtained in the embodiment illustrated in Fig. 5.\|[0072] Also in Fig. 5, an alternative ammonia absorption recovery process is utilised. In this embodiment, as the final product slurry rises from the underground chamber 70, the static head it experiences may decrease. A consequence of this is that the boiling point temperature will fall, eventually below that of the slurry rising in the products pipeline, leading to the flashing of some of the water to steam, and the stripping of ammonia from solution. As ammonia comes out of the solution as a gas it will absorb latent heat from the final product slurry, partially cooling it; the temperature would tend to track the boiling point of water at the prevailing pressure. The bubbles of ammonia will reduce the average density of slurry in the hot products pipeline to below that in the incoming reactants pipeline, leading to a pressure differential in the system that would serve to drive the circulation of the reactant and product slurries from the CO2 Absorber 30 and through the underground chamber 70, heat exchangers and other items of process plant. As shown on Fig. 5, the ammonia recovery vessel 78 and other necessary plant and equipment for recovering ammonia from the product slurries are installed at a level (perhaps 150 metres below ground level) that facilitate the use of static head to maintain a pressure in the vessel 78 of around 15 Bar, i.e. high enough so that ammonia was a liquid at near-ambient temperatures.\|[0073] As for the pipeline reactor case, the ammonia will be discharged as a gas from the top of the vessel 78, however due to the circumstances outlined above, this vessel 78 could be much simpler in design and, in an embodiment, need be little more than a gas-liquid separator. While some additional heat energy may be required to recover essentially all of the ammonia as a gas, typically as steam, with the arrangements proposed the heat-energy burden of carbon sequestration could be greatly reduced.\|Examples\|[0074] Again with specific reference to Fig. 2, a non-limiting example process flow for carbon sequestration for the first system configuration 10 described herein (i.e. the system depicted in Fig. 1) will now be given, wherein for convenience, like parts to those shown in the foregoing embodiment have been numbered with like numerals.\|Example 1\|[0075] Table 1: Indicative mass and heat balance figures from 1.000 MWe of black coal-fired electricity generation plant.MaterialPer yearPer hourTotal CO2 generated:6.4 106 t800 tSilicate rock to absorb 90% of this CO2:145m 106 t1,800 tWater required to make 30% by wt slurry:33.6 106 t4,200Ammonia to conv. 90% of CO2 to (NH4)2CO3:4.45 106 t560 tHeat liberated (3.6 GJ/t CO2):2,800 GJTotal slurry with (NH4)2CO3:58 106 t7,2501Slurry density:1.3 t/m31.3 t/m3Slurry pipe dia. (both with 2 m/s velocity:1.0 m1.0 metresAmmonia pipe diameter, 2 m/s velocity0.4 m0.4 metresConc. of ammonia in Absorber aq. phase:12% (by wt)12%Ammonia lost due to SOx16,000 t2.0 tAmmonia lost due to NOx3,000 t0.37 tOther losses of ammonia:11,000 t1.38 tAmmonia make-up % of flow to Absorber:0.67%0.67%\|[0076] Table 1 provides a detailed mass and heat balance for a carbon dioxide sequestration process, assuming:\| 90 per cent carbon dioxide capture and sequestration from 1,000 MWe of black coal-fired electricity generation plant, which when operating in base-load mode might expect to generate annually 8,000 GWh of electricity;\| where on a dry ash-free basis, the coal is 81.3% by weight carbon and 0.65% sulphur (as S) and the flue gases contain 400 ppm NOx.\|[0077] The heat of formation of ammonium carbonate in solution from ammonia, water and carbon dioxide is around 2.0 GJ/tonne carbon dioxide equivalent, sufficient to heat the slurry by 75°C. Offsetting this is the heat absorbed when each tonne of ammonia is vaporised in the absorption zone, around 1.0 GJ/tonne ammonia. This is equivalent to around 1.8 GJ per tonne of carbon dioxide absorbed, sufficient to cool the slurry feed by around 60°C. It follows that there would be an overall temperature rise between the time the slurry feed enters the absorption zone and the time it enters the return pipeline 52, of around 15°C. In practice, it may be necessary to design the process so that the last slurry feed that the final largely carbon dioxide free flue gases is the coldest: less than 5°C.\|[0078] As well, the heat released when ammonium carbonate in solution reacts with the silicate rocks, roughly 1.45 GJ/tonne carbon dioxide absorbed, is sufficient to raise the temperature of the slurry feed by around 55°C. This occurs in the return pipeline 52.\|[0079] At the mine, the condensation of around 300 tonnes per hour of ammonia would release some 160 MWt of heat energy, which can be rejected to the environment via a cooling tower.\|[0080] An advantage of the carbon dioxide sequestration process 100 and systems 10, 20 according to embodiments of the present invention is that by selecting ammonia as a catalyst/promoter, a single integrated process can be provided for both capture and sequestration of carbon dioxide. In an embodiment, sequestration of the carbon dioxide takes place in a reactor, in the form of a return pathway 52 of a pipeline 44, which advantageously connects the power station (i.e. the source of carbon dioxide) to the source/destination of the absorbent material being used in the process. In an alternative embodiment, where geological conditions permit, the reactor may take the form of an underground chamber which advantageously facilitates the reaction without requiring pressure-exchange and head-recovery equipment required for the pipeline embodiment. Another advantage of the carbon dioxide sequestration process and systems is that the reaction kinetics may be improved by using ammonia. Therefore, by using ammonia and exploiting the heat generated by the exothermic reaction, the energy consumption of the process 100 can be kept to a minimum. As the reaction products are thermodynamically stable, carbon dioxide can be stored in a permanent stable solid form. Following from this, further advantages include lower operating and capital costs.\|[0081] Persons skilled in the art will appreciate that further advantages may arise from carrying out certain steps of the aforementioned embodiments in isolation. For example, the catalytic effect of a solution of ammonia with an ammonium salt (that may be ammonium carbonate formed by exposing an ammonia-rich solution to a gas stream containing carbon dioxide) in the carbon dioxide sequestration process can also be utilised for extracting metals (e.g. magnesium, iron, nickel, copper and other metals present in the silicate rock) from metal silicates, such as magnesium-rich metal silicates. In such an embodiment a solution comprising ammonia and ammonium may be mixed with a metal silicate (typically in slurry form) to allow the dissolution of magnesium ions by ammonia to recover the metal, in this embodiment a metal compound in the form of magnesium carbonate. The mixing may occur in an ammonia absorption chamber such as that previously described in connection with the preceding embodiments. Preferably the ammonia solution comprises concentrated ammonia in the presence of ammonia salts in solution, such as ammonium carbonate, to prevent the precipitation of magnesium hydroxide, hence allowing the dissolution of magnesium ions by ammonia to continue. A further advantage arising from this process is that after extraction of magnesium carbonate, other minerals (metals) present within the silicate rock are also amenable to recovery. The silicate rock may comprise mafic or ultra-mafic rocks (i.e. rocks with a high magnesium content).\|[0082] The catalytic effect of the ammonia follows from its tendency to form complexes (ammines) with certain metal ions including magnesium (Mg2+), divalent iron (Fe2+), copper (Cu2+) and nickel (Ni2+). The presence of ammonium salts notably the carbonate formed from the reaction between ammonia and carbon dioxide prevents precipitation of the otherwise insoluble magnesium hydroxide. Magnesium carbonate is however insoluble in such an environment, so a precipitate of this compound will form from the reaction between magnesium hydroxide and ammonium carbonate, to yield ammonium hydroxide and free ammonia in solution, the latter continuing to extract additional magnesium and other metals from the silicate rock through formation of ammine complexes until all such susceptible metals have been extracted.\|[0083] Subsequently, the ammonia is recovered from the solution by in the ammonia recovery vessel, a consequence being a progressive reduction in the concentration of free ammonia in the reactive slurry. This leads to destruction of the metal ammine complexes, but in a progressive manner, depending on the stability of the complexes, which stability in turn differs between metals. Those of magnesium are relatively weak (the reason most of the magnesium will have precipitated out as magnesium carbonate), so the first salt to be precipitated is further magnesium carbonate. As the concentration of ammonia in solution continues to fall, other metals can precipitate in sequence, allowing the opportunity of obtaining precipitates of each single metal in relatively pure form.\|[0084] Finally, it is to be appreciated that various alterations or additions may be made to the parts previously described without-departing from the spirit or ambit of the present invention as defined by the following claims. The process is not limited to having a single two-stage continuous reactor, or a single tube-like reactor, as the process may be arranged to utilise alternatively configured items of equipment as necessary to accommodate process variables, arising from different source materials, capital and operating costs. For example, in the exemplary embodiment previously described the plant design is based on the emission of 800 tonnes CO2/GWh generated from a state-of-the-art black coal-fired electricity generation plant. By comparison, the Bayswater Power Station and the Liddell Power Station, both in the Hunter Valley of New South Wales, Australia, able to generate 2,640 MWe and 2,040 MWe respectively, being older hence less efficient can be expected to emit between 850 and 900 tonnes CO2/GWh.\|[0085] Thus the concentration and rate of carbon dioxide emissions in the flue gas emitted by the power plant may vary such that the plant equipment design may be reconfigured to accommodate these variables. For example, alternative equipment can be configured for the various heat and pressure exchange stations. The carbon dioxide absorption zone and the scrubbing zone may be arranged in series in two separate vessels (rather than the nested configuration shown in Fig. 1). The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s). As well, the corresponding solids concentration in the slurry feed may be higher or lower than 30% solids by weight. It is possible that the metal silicate solution may comprise a blend of metal silicates, e.g. mixture of serpentines and olivines, even pyroxenes. The reaction kinetics may require heat to be removed from the reactive solution (rather than heat addition as described above). These factors will impact and alter the system pressures. There might be two or more pipelines for transporting the metal silicate solution and the reactive solution; because there are more pipelines additional heat exchangers and pressure-exchange apparatus may be used. The power station flue gas may include additional pre-processing steps including flue gas desulphurisation (FGD) and selective catalytic reduction (SCR) to reduce concentrations of SOx and NOx respectively hence losses of ammonia from the system. Furthermore, the availability of services, such as steam and cooling water may require different equipment arrangements.\|[0086] Any reference to prior art contained herein is not to be taken as an admission that the information is common general knowledge, unless otherwise indicated.\|[0087] In the claims which follow and in the preceding description of the invention, except where the context requires otherwise due to express language or necessary implication, the word "comprise" or variations such as "comprises" or "comprising" is used in an inclusive sense, i.e. to specify the presence of the stated features but not to preclude the presence or addition of further features in various embodiments of the invention.	(EP2134449)\|Technical Field\|[0001] This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|Background to the Invention\|[0002] There is increased focus on reducing carbon dioxide emissions to the atmosphere, to help minimise the effects of global warming. Carbon dioxide sinks exist naturally, with the main naturally occurring sink being the ocean. Plants are also an effective form of carbon dioxide sink and use photosynthesis to remove carbon from the atmosphere by incorporating it into biomass. However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\|[0003] The major source of harmful carbon dioxide gases are large fossil fuel power stations which, when fuelled by black coal, on average typically output around 0.8 to one tonne of the gas for each MegaWatt-hour (MWh) of electricity they generate. For example, a large power station such as the 2,640 MW Bayswater in the Hunter Valley of New South Wales, Australia, in generating 20 million MWh of electricity in a year, would also output 18 million tonnes of carbon dioxide. It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations. It would also be advantageous if a system and method were provided for the disposition of the gas to be independently audited.\|[0004] Known methods of sequestering carbon dioxide are described in WO 2006/008242, WO 200=4/0940=t3, WO 2005/108297 and WO 200=4/0987=40. WO 2006/022885 describes a method of ultra-cleaning a combustion gas, followed by capture and regeneration of carbon dioxide. The application does not describe a process in which a reaction between a metal silicate is controlled to produce a metal carbonate. There is also no disclosure of absorbing carbon dioxide in an ammoniated slurry that contains a metal silicate dispersed through it.\|Summary of the Invention\|[0005] In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|[0006] It should be noted that the terminology "gas stream containing carbon dioxide" does not mean that the stream contains only carbon dioxide, and may contain other off gases.\|[0007] In an embodiment of step (i), pressurised liquid ammonia is charged into the metal silicate slurry in such a manner that the liquid ammonia partially flashes to a vapour to produce the ammonia/metal silicate slurry.\|[0008] An embodiment of step (ii) may comprise exposing the carbon dioxide-containing gas stream to a spray of the slurry.\|[0009] An embodiment of step (iii) may comprise elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\|[0010] In an embodiment, the reactor is a pipeline. The pipeline preferably comprises multiple flow paths. In an embodiment, the reaction takes place along the length of one of the flow paths. Another of the flow paths may be utilised to supply the metal silicate slurry to the first stage.\|[0011] In an embodiment, the method comprises the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\|[0012] In an embodiment, the reactor is a chamber located in use underground. Preferably, the chamber is located at a depth that provides sufficient pressure to enhance the reaction between the carbon dioxide and the metal silicate. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0013] In an embodiment, the method may also comprise the step of recovering ammonia resulting from the reaction stage (iii) and recycling it to the first stage. In an embodiment, an alkali is added to the final product prior to performing the step of recovering ammonia. The alkali may be power station fly ash or pulverised bottom ash obtained by filtering or otherwise cleaning the carbon dioxide-containing flue gas stream. The ammonia may be recovered as both a liquid and a gas, with the liquid being converted partially to a vapour for recycling in the first stage and the gas being extracted, condensed and mixed with the metal silicate before it is supplied in the first stage.\|[0014] In an embodiment, the step of recovering the ammonia is effected in a recovery vessel which is pressurised to facilitate the recovery of ammonia in liquid form at ambient temperatures. In an embodiment, the recovery vessel is in use located at a depth sufficient for achieving the pressure to recover the ammonia in liquid form. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0015] In an embodiment the process comprises the further step of grinding a metal silicate rock to produce the metal silicate slurry. The metal silicate slurry may comprise 30 to 60% finely ground solids by weight. In an embodiment, the metal silicate is a magnesium-rich silicate mineral. The magnesium rich silicate may be comprised of a serpentine- and/or olivine- and/or pyroxene-rich mineral.\|[0016] In accordance with a second aspect, the present invention provides a system for sequestering carbon dioxide from a gas stream, the system comprising:\| (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and\| (b) a reactor for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|[0017] In an embodiment, the first apparatus comprises an ammonia absorption chiller arranged to (a) chill the metal silicate slurry and (b) mix the chilled slurry with ammonia to produce the ammoniated slurry. In an embodiment step (a) is carried out prior to step (b).\|[0018] The reactor may comprise the pipeline as set forth in the first aspect. In an alternative embodiment, the reactor may comprise the chamber as set forth in the first aspect. The metal silicate may comprise a magnesium rich silicate as set forth in the first aspect. In an embodiment, the system comprises a recovery vessel arranged to recover ammonia contained in the metal carbonate product.\|[0019] In accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the carbon dioxide to react with the metal silicate and produce a metal carbonate.\|[0020] In accordance with a fourth aspect of the present invention there is provided a method for causing a slurry, comprising carbon dioxide absorbed in an ammonia/water/metal silicate slurry, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the carbon dioxide and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|[0021] In an embodiment, the slurry provided to the chamber is the reactive slurry produced in the process as set forth in the first aspect. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0022] In an embodiment, the method comprises the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber. In an embodiment, the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.\|[0023] In accordance with a fifth aspect there is provided a power station utilising a carbon sequestration system in accordance with the second aspect, the system arranged to sequester carbon dioxide from flue gas emitted by the power station.\|[0024] In accordance with a sixth aspect, in an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, there is provided the steps of: (i) prior to passing ammonia to the absorption process, allowing the ammonia in pressurised liquid form to expand in an evaporator stage so as to provide a cooling effect in that stage; and (ii) passing the water/metal silicate slurry through the evaporator stage so as to chill said water/metal silicate slurry, prior to mixing it with the ammonia in the ammonia absorber process.\|[0025] In an embodiment, the process comprises the further step of providing the ammoniated slurry to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammonia/water/metal silicate slurry to thereby absorb the carbon dioxide into a reactive slurry.\|[0026] In an embodiment, the process comprises the further step of passing reactive slurry which is to be re-circulated through the scrubbing chamber through the evaporator stage prior to re-circulation. The evaporator stage may be implemented in an evaporator chamber. The scrubbing stage may be implemented in the first apparatus, as set forth in the second aspect.\|[0027] In accordance with a seventh aspect of the present invention there is provided an ammonia absorption chamber arranged to implement the process as set forth in the sixth aspect.\|[0028] In accordance with an eighth aspect of the present invention there is provided a method of extracting a target metal from a metal silicate comprising the step of mixing the metal silicate with a solution that comprises ammonia and ammonium salt, whereby the ammonia reacts with the metal silicate to cause the target metal to dissolve into the solution.\|[0029] In an embodiment the method comprises the further step of grinding the metal silicate and forming it into a slurry prior to mixing the metal silicate with the solution.\|[0030] In an embodiment the mixing takes place in an ammonia absorption chamber.\|[0031] In an embodiment the metal silicate is a magnesium-rich silicate.\|[0032] In an embodiment the magnesium-rich silicate is a serpentine and/or olivine and/or pyroxene silicate metal.\|[0033] In an embodiment the ammonium in solution comprises ammonium carbonate.\|[0034] In an embodiment the target metal dissolves into the solution and then precipitates as a metal carbonate to be removed for recovery.\|[0035] In an embodiment the target metal is one or more of magnesium, iron, copper and nickel. The dominant metal within the metal silicate may comprise magnesium.\|[0036] In a ninth aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a chilled slurry of a metal silicate rock with ammonia so as to produce a chilled ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the chilled solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|Brief Description of the Drawings\|[0037] An embodiment of the present invention will now be described, by way of example only, with reference to the accompanying drawings, in which:\| Fig. 1 is a schematic of a carbon dioxide sequestration system according to an embodiment of the present invention;\| Fig. 1A is a further schematic of a carbon dioxide sequestration system according to an embodiment of the present invention with additional detail of the Residual Ammonia scrubber, Ammonia absorber, and CO2 absorber shown.\| Fig. 2 is a process flow diagram showing a method of sequestering carbon dioxide using the system of Fig. 1, in accordance with an embodiment of the present invention;\| Fig. 3 is a schematic of a pressure exchange apparatus utilised by the carbon dioxide sequestration system of Fig. 1, in accordance with an embodiment of the present invention;\| Fig. 4 is a schematic of a heat exchange apparatus utilised by the carbon dioxide sequestration system of Fig. 1, in accordance with an embodiment of the present invention; and\| Fig. 5 is a schematic of a carbon dioxide sequestration system, according to an alternative embodiment of the present invention.\| Fig. 5A is a further schematic of a carbon dioxide sequestration system, according to an alternative embodiment of the present invention with additional detail of the Residual Ammonia scrubber, Ammonia absorber, and CO2 absorber shown.\|Detailed Description of an Embodiment\|[0038] In the following description, an embodiment of the present invention is described in the context of a system, apparatus and method for the capture and sequestration of carbon dioxide contained within flue gases emitted by a fossil fuel-fired power station. However, it is to be understood that the system, apparatus and method could equally be utilised for the permanent sequestration of carbon dioxide from any source and is not limited to the particular arrangement described herein.\|[0039] With reference to Fig. 1 there is shown a flow diagram of a system 10 for performing a carbon dioxide (CO2) sequestration process from a gas feed stream containing carbon dioxide outputted from a power station, in accordance with an embodiment of the present invention. With additional reference to Fig. 2, the system is arranged to perform the process 100 of (i) in a first stage, mixing a slurry of chilled ground metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the ammonia/water/metal silicate solution to thereby absorb the carbon dioxide into a reactive solution; and (iii) passing the reactive solution through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate and by-product silica (stage three).\|[0040] In an embodiment, the slurry of ground metal silicate rock is chilled by circulating the slurry through a vessel in which ammonia evaporates. In an embodiment another stage is carried out prior to stage (ii), namely contacting flue gases in a vessel in a counter-current, staged manner so that residual ammonia in the flue gases is scrubbed from these gases to levels low enough to allow their final discharge in the atmosphere.\|[0041] In the illustrated embodiment the three stages are performed successively, with the first two stages occurring within a first apparatus 20 in the form of two separate reaction chambers, namely an absorption chamber 28 and a scrubbing chamber 30, and the last stage occurring within a reactor in the form of a pipeline 52 which may, for example, connect the mine site to the power plant. As will be described in detail in subsequent paragraphs of the specification, the reactor may alternatively take the form of an underground chamber (see Fig. 5) excavated at a sufficient depth to facilitate the conditions for the carbonation reactions to take place.\|[0042] The carbon dioxide sequestration process utilised in embodiments of the present invention is based on mineral carbonation. Mineral carbonation is a reaction between a metal-oxide bearing material and carbon dioxide. The metal-oxide bearing material may for example be alkaline-earth metals. Advantageously, the process 100 does not require the source of carbon dioxide to be particularly pure. In mineral carbonation, carbon dioxide reacts with the metal oxide bearing material to generate insoluble carbonates, that is to say:\| MO + CO2 → MCO3 + heat (1)\|which is an exothermic reaction, occurring more rapidly at elevated temperature, typically above 200°C. Certain chemicals may serve to increase the rate at which this reaction proceeds without being consumed themselves, i.e. they serve as catalysts. The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|[0043] The exact nature of the insoluble carbonates formed by the reaction depends on the metal-oxide bearing material. Suitable materials may be naturally occurring alkaline-earth metal-rich silicate rocks which contain mineral constituents such as serpentinite (Mg3Si2O5(OH)4), olivine (Mg2SiO4), orthopyroxene (MgSiO3), talc (Mg3Si4O10(OH)2) and wollastonite (CaSiO3). In practice, the element Iron (Fe) may substitute for some of the Magnesium (Mg) or Calcium (Ca). Other suitable materials include alkaline industry residues such as slag from steel production, the ash (both fly and bottom) from pulverised coal-fired boilers, the ash remaining from the combustion of paper recycling residues (de-inking ash), and cement. The amount of heat generated in the reaction will depend on the specific metal and on the mineral containing the metal oxide as can be seen below in the case of three natural silicates (heat values are given per unit mole of CO2 and at standard conditions (25°C and 0.1 MPa):\| Olivine\| Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 + 89 kJ mol-1 CO2 (2a)\| Serpentine\| Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol-1 CO2 (2b)\| Wollastonite\| CaSiO3 + CO2 → CaCO3 + SiO2 + 90 kJ mol-1 CO2 (2c)\|[0044] A preferred silicate rock (because of its greater abundance in continental land masses) comprises the mineral serpentine, Mg3Si2O5(OH)4, All of these minerals may be pre-treated to increase the surface area of rock that can come into direct contact with the carbon dioxide. In an embodiment, the pre-treatment involves crushing, grinding and/or milling of the mineral, as well as some mechanical classification and separation. Typically, these minerals would be wet-milled in ball mills or equivalent to form a finely ground metal silicate slurry (hereafter 'silicate slurry') 36 wherein 90% of the mineral matter was finer than 40 microns. However, the extent of the pre-treatment is dependent upon the source and type of mineral(s) being used in the process.\|[0045] With specific reference to Fig. 1, the carbon dioxide sequestration system 10 will now be described in detail. The system 10 receives a raw flue gas mixture feed stream 32 that has been generated and subsequently emitted by a power station (not shown). In the embodiment described herein, the raw flue gas mixture 32 is passed though a filter 34 to remove particulate matter. Suitable filters may include fabric filters, electrostatic precipitators and the like. Cleaning the raw flue gas mixture 32 serves to minimise both the maintenance costs in downstream gas-handling equipment and the concentrations of particulates in flue gases ultimately discharged to the atmosphere. It will be understood, however, that while desirable for process reasons, it is not essential that the raw flue gas mixture 32 be cleaned of particulates before it enters the scrubbing chamber 30.\|[0046] To maximise heat recovery in the system 10, the filtered flue gas mixture is then passed through a heat exchange apparatus in the form of a heat exchanger 34 so that the sensible heat of the filtered flue gas mixture (typically emitted at a temperature of around 135°C) is exchanged with the cooler gasses being expelled from the scrubbing chamber 30 of the first apparatus 20 and the filtered flue gas mixture is cooled to its water-vapour saturation temperature (i.e. to about 50°C). Suitable heat exchangers may include, for example, recuperative-type heat exchangers, such as the Ljungstrom rotary design as used for air pre-heating in power stations.\|[0047] As mentioned in preceding paragraphs, the carbon dioxide sequestration system 10 receives a source of silicate slurry 36. According to the embodiment described herein, the silicate slurry source is located near or at the mine site from which the silicate rocks are sourced. As previously described, the silicate mineral sourced from the mine site is finely ground (preferably by wet-milling in ball mills or equivalent to form the slurry) wherein 90% of the mineral matter is finer than 40 microns. The silicate slurry 36 is subsequently passed through a first pressure-exchange apparatus 38. To minimise power consumption, the pressure of the silicate slurry 36 may be increased by exchanging pressure with the final metal carbonate/silica product (hereafter `final product'), typically to a pressure of approximately 10 Bar. In addition, to minimize heat losses from the system 10 (and to ensure that the final product is cooled to a suitable temperature before it is emplaced in its final permanent repository), the silicate slurry 36 passes counter-currently through a second heat exchanger 40 to absorb the surplus sensible heat contained in the final product. At a second pressure-exchange apparatus 42, the pressure of the silicate slurry 36 is further increased, this time to a substantially higher level (typically 100 Bar). Again, this boost in pressure is achieved by exchanging pressure, but this time with the carbonate/silica slurry prior to it undergoing treatment in the ammonia gas recovery vessel 54 (as will be described in detail in subsequent paragraphs).\|[0048] A pipeline 44 connects the first apparatus 20 to the mine site and is used to transport the silicate slurry 36 used in the sequestration process 100. As will be described in more detail in subsequent paragraphs, an alternate path 52 in the pipeline 44, in this embodiment, also serves to act as a controlled reactor in which the metal carbonate reaction largely takes place. At or near to the power station site, the silicate slurry 36 is passed counter-currently through a third heat exchanger 46 and a third pressure-exchange apparatus 48, where the silicate slurry 36 is cooled and reduced in pressure by exchange with the reactive slurry discharged from the first apparatus 20, before being fed directly into the evaporator vessel 82, where ammonia which has passed through the expansion valve 29 and is now at a very low temperature, cools the silicate slurry to near freezing. To ensure that the silicate slurry 36 is not actually frozen, a portion of this slurry is circulated through the evaporator vessel. The chilled silicate slurry passes downwards through a vessel, the residual ammonia scrubber, in such a way that cleaned and cooled flue gases that have been stripped of most of their carbon dioxide content, pass upwards from below. There may be as many as six counter-current contacting stages, such that the cleaned, largely carbon dioxide-free flue gases may leave the system with less than one part per million of ammonia.\|[0049] The silicate slurry, now charged with any ammonia arriving in flue gases from below, enters the ammonia absorber 28, where it absorbs into solution all of the ammonia that is recovered in the ammonia recovery vessel 54 so as to produce a ammonia/water/metal silicate slurry.\|[0050] The ammonia is recycled from the ammonia gas recovery stage of the process (described in subsequent paragraphs), with additional quantities required only to make up for losses, which should be small. Recovered liquid ammonia (which may contain small amounts of water) is supplied to the absorption chamber 28 by way of a pipeline 60, under pressure. In a preferred embodiment, pressurised liquid ammonia passes through the pressure reduction valve 29, which reduces its pressure to near atmospheric, at which pressure it discharges into a vessel, the evaporator chamber 82, prior to entering the absorption chamber 28. A portion of the ammonia will flash to vapour upon entering the evaporator chamber 82. The ammonia, in vaporising, absorbs substantial quantities of latent heat which is withdrawn from the slurries circulating through banks of tubes in the evaporator chamber 82, thereby chilling them to near freezing. In the embodiment shown in Fig. 1, the heat absorbed as the ammonia vaporises is drawn from the silicate slurry used as the residual carbon dioxide scrubbing medium in the residual ammonia scrubbing chamber. This is to ensure that the scrubbing medium last in contact with the cooled, filtered flue gases is the most chilled.\|[0051] The vaporised ammonia flows from the evaporator chamber 82 directly into the ammonia absorption chamber 28, wherein it is rapidly absorbed into the deluging spray of circulating silicate slurry 36 after this has passed downwards through the several stages of the residual carbon dioxide scrubber, to produce the ammonia/water/metal slurry used as the circulating scrubbing medium for the carbon dioxide scrubbing chamber 30. When the ammonia is absorbed in the silicate slurry 36 a substantial quantity of heat is liberated: the heat of solution of ammonia gas in water. Much of this heat is removed as the slurry circulates through the heat exchanger 84. As illustrated, the heat exchanger 84 and cooling tower also serve to remove much of the excess low-grade heat generated from the absorption of the ammonia in the silicate slurry.\|[0052] The cooled filtered flue gas mixture passing through the heat exchanger 34 enters the scrubbing chamber 30 where the gas mixture passes upwards through deluging sprays of absorbent slurry, the absorbent slurry having been drawn from the ammonia absorption chamber 28 and discharged into the head space of the scrubbing chamber 30. When carbon dioxide is absorbed in the ammonia/water/metal silicate slurry, a further substantial quantity of heat is liberated, as carbon dioxide and ammonia form in solution a series of ammonium carbonate compounds. With sufficient ammonia supplied to the absorption chamber 28 to achieve 90 per cent capture of carbon dioxide, the tendency will be to form the bicarbonate NH4HCO3 in preference to the normal carbonate (NH4)2CO3 and the carbamate, NH2COONH4, which will also be present in smaller quantities, perhaps along with some urea, CO(NHZ)2. The system 10 is configured such that the coldest slurry will be the last to contact the stripped (of carbon dioxide) flue gas mixture, in such a way that ammonia slip (losses in final flue gases to the atmosphere) are essentially eliminated. In the embodiment shown in Fig. 1, the scrubbing chamber 30 is shown as being constructed separately to the absorption chamber 28. Suitable scrubbing chambers may be generally similar to the type used for flue gas desulphurisation.\|[0053] As previously described, the sensible heat is removed from the filtered flue gas mixture in the first heat exchanger 34, cooling it to around 50°C, before entering the scrubbing chamber 30. The clean flue gases exiting the scrubbing chamber 30 typically comprise around 95 per cent nitrogen and inerts by volume. The balance comprises some oxygen and around 1.5 per cent carbon dioxide, being the remnant quantity of this gas after some 90 per cent had been stripped out in the scrubbing chamber 30.\|[0054] The resultant product of this two-stage process is a reactive solution in the form of a metal silicate slurry in an aqueous phase that is itself primarily a solution of ammonium carbonates. A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor. On route to the mine site, at or near to the power station, the reactive slurry is pressurised at the third pressure-exchange apparatus 48 to a high pressure of around 120 Bar (above the critical pressure of ammonia) and also heated to close to the boiling point of water at the pressure in question. Heating is accomplished firstly by transferring heat from the incoming silicate slurry arriving from the mine at the heat exchanger 46, and also by injection of steam 54. Without being bound by theory, the inventor anticipates that, subject to the process design assumptions of Example 1 (see table below), around 600 tonnes per hour of steam would be required to raise the temperature of the reactive slurry by around 100°C, to say 225°C, at which temperature the carbonation reactions are likely to reach acceptable rates. Heat liberated from the reaction between carbon dioxide and the metal silicate in the reactive slurry, which is highly exothermic, is capable on its own of raising the reactive slurry temperature by around 75°C (under the assumptions made in respect of Example 1), to yield a final temperature of some 300°C by the time the reactive slurry reaches the vicinity of the mine site, or site of other final emplacement. This temperature rise would be obtained despite some losses along the length of the return pipeline 52, notwithstanding attempts to minimise such losses by cladding this pipeline 52 throughout its length by suitable insulation (lagging).\|[0055] In the return pipeline 52 of the pipe reactor, most if not all of the carbon dioxide present in the reactive slurry can react with the silicate minerals and convert to insoluble carbonate during approximately the few first hours of transit. Each hour may correspond to a 10 kilometre length of this pipeline. In practice, however, the power station and the mine site may be much more than this distance apart, thereby allowing more than adequate time for reactions to proceed essentially to completion resulting in the metal carbonate product that contained most if not all of the carbon dioxide originally scrubbed from the power station flue gases. A high concentration of ammonia is maintained in the slurry throughout its passage from the power station to the mine/quarry or other emplacement site.\|[0056] When the final product in the return pipeline 52 reaches the vicinity of the mine site, as described above, it is passed through the second pressure-exchange apparatus 42 to lower the pressure of the stream from perhaps as high as 120 Bar to around 15-20 Bar, before entering the ammonia gas recovery vessel 54. With the temperatures indicated on Fig. 1, all of the ammonia and some of the water flash to vapours (the water would boil, the ammonia being driven out of solution) as the final product enters the ammonia gas recovery vessel 54, a consequence of a drop in temperature of more than 100°C. As shown in Fig 1, the hot pressurised final product transfers its sensible heat to the contents of the ammonia gas recovery vessel 54. This heat input assists to maximise the system's efficiency, as stripping the ammonia from the product as a gas absorbs considerable heat energy. To minimize the waste products generated by the system 10, and prior to entering the pipeline 44 for delivery to the continuous reactor 22, silicate slurry from the mine site is fed and re-circulated in the residual ammonia absorber 56 where residual vapours from the ammonia gas recovery vessel 54 are passed. A gas phase stream exiting from the top of the ammonia gas recovery vessel 54 contains essentially all of the free ammonia, which along with some water vapour condenses out in a condenser 58 to form a liquid phase that is mostly ammonia. In an embodiment, the condenser 58 is cooled by circulating water from dry (e.g. radiator-type) cooling towers, fin fan coolers, or, because no fans are required, a natural-draft cooling tower (not shown) such as used for cooling in the power station. This recovered liquid ammonia, representing the bulk of the ammonia injected into the circulating slurry in the absorption chamber 28, flows under pressure (aided by pumps, not shown) through an overland ammonia pipeline 60 to the power station site.\|[0057] The final product carbonate slurry (containing nearly all of the carbon dioxide in the original power station flue gases but now sequestered as carbonates), leaves the bottom of the ammonia gas recovery vessel 54. The final product slurry is free of ammonia, and in a form suitable for permanent emplacement in mine voids or other purpose-built repositories (not shown). In these emplacements the solids can settle and consolidate, releasing much of the aqueous phase as a clear supernatant. This supernatant may be collected and re-used in the process, for example, to prepare the silicate slurry 36 and returned to the power station site, via pipeline 44.\|[0058] It should be noted that not all of the ammonia added in the first apparatus 20 can be recovered and returned to the process via the overland ammonia pipeline 60. Some ammonia may end up as ammonium salts: sulphites and sulphates, and as ammonium nitrites and nitrates, from SOx and NOx respectively in the raw flue gases. If the raw flue gas source is a flue gas generated by a typical fossil fuel-fired power station, and assuming use of modern low-NOx burners, losses of ammonia via these reactions should will be minor. Their presence in the final carbonate product slurry may furthermore, assist with rehabilitation of the final emplacements of the carbonate minerals. Figure 1A illustrates an alternative embodiment including a residual ammonia scrubber positioned within the scrubbing chamber 30.\|[0059] It may be desirable to reduce the losses of ammonia that would occur in this way. In an embodiment, this is achieved by dosing, or otherwise adding to the reacted slurry immediately prior to its entry into the ammonia recovery vessel 58, an appropriate quantity of slaked lime or other suitable alkali. A source of such alkali may be power station fly ash or pulverised bottom ash. The presence of limestone or dolomite in the original coal may render them suitable for this duty; in passing through the boilers much of this limestone or dolomite will be converted to alkalis suitable for ammonia recovery: quicklime or dolime (dolomite-lime), respectively.\|[0060] Should it arise that the content of limestone or dolomite in the coal fuel is inadequate for the duty (as is likely to be the case with most power station fly ashes), it is possible to dose the appropriate quantity of pulverised limestone or dolomite to the power station boilers (not shown). This dosing may be conducted at a location in the hot combustion gas path where the gas temperatures are in the range 800-1,000°C, i.e. sufficient to convert these minerals to the reactive oxide forms (lime, or dolime respectively). For example, this may occur upstream of the boiler's economiser. When the ammonia-recovery vessel is close to the power station, as it would be in the case of the underground chamber reactor embodiment (Fig. 5), it may be appropriate to add all of the power station fly ash to the final product slurry to maximise the regeneration of ammonia for re-use in the process. In this manner, both fly ash and the final product slurry from the carbon sequestration process may be handled and co-disposed of as a single stream. An anticipated advantage stemming from the presence of fly ash having pozzolanic properties (a tendency to set in the presence of alkalis and moisture) in the final product, will assist with the rehabilitation process, by encouraging the final product/fly ash mix to "set".\|[0061] With reference to Fig. 3, there is shown an arrangement for the pressure-exchange apparatus described above. At the end of the reaction process, the pressure of the final carbonate-rich product must be reduced from approximately 120 Bar to atmospheric pressure. As described above, this is undertaken in two stages: from 120 Bar down to around 15 Bar, a pressure suitable for operation of the ammonia recovery stage, then from 15 Bar down to atmospheric pressure. Instead of merely reducing pressure by throttling valves, thereby losing the energy embodied in this pressure, the energy this pressure represents may be conserved by transferring it to the extent possible, in two stages, to the silicate slurry. In Fig. 3, slurry A comprises the products of the reactions that occur as the ammoniated, carbonated silicate slurry flow through the pipeline 44 from the power station to the mine site; while slurry B represents silicate slurry from the mine. A consequence of pressure exchange in these two stages is that slurry A's pressure would fall from around 120 Bar to near ambient pressure, while that of slurry B would rise: in the first stage (working from right to left) to around 10 Bar, then to perhaps 100 Bar in the second stage.\|[0062] Another pressure-exchange apparatus is also utilised at the power station site. Here, using the terminology of Fig. 3, slurry A represents the hot silicate slurry arriving via the pipeline from the mine; while slurry B comprises slurry exiting the scrubbing chamber 30 (i.e. silicate slurry now charged with ammonia and carbon dioxide, but at close to ambient pressures). A consequence of pressure exchange in this stage is that slurry A's pressure would fall from its arrival pressure (this may be 120 Bar, a pressure that would be maintained by booster pumping stations at strategic locations (not shown) along the pipeline 44 to overcome friction losses), to near ambient pressure. This pressure may be transferred (exchanged) to the extent possible to slurry B, thereby minimising the amount of pumping energy required to raise the pressure of this slurry to the levels required, here assumed to be 120 Bar. Since slurry A at this point will be at well below 120 Bar, pressure-exchange between slurries A and B alone may not be capable of raising the pressure of slurry B to 120 Bar. Also, the volume of slurry B may exceed that of slurry A. This is because of the much higher contents of carbon dioxide and ammonia, and of water condensed out of the power station flue gases. In an embodiment, additional pumping capacity may be installed to boost slurry B pressures to those required for the pipeline 44, and to pressurise those (relatively small) quantities of slurry B that cannot be pressurised by pressure-exchange with slurry A. For this function, conventional high-pressure diaphragm pumps, such as the Geho pump manufactured by Weir Netherlands b.v., may be implemented. This pumping, together with the pumping energy required to maintain pressures along the length of the pipelines, account for a substantial proportion of the total mechanical energy input to the total process. Other suitable pressure exchange/pump-turbine sets may comprise centrifugal pumps and radial-type hydraulic turbines. As the pressures are relatively high, the type of centrifugal pump may be a multi-stage barrel-type pump.\|[0063] With reference to Fig. 4 there is shown a configuration for the heat exchanger arrangements 40 & 46, according to an embodiment of the present invention. As previously discussed, high temperatures are required to initiate and accelerate the carbon sequestration reactions: the conversion of silicates to carbonates. These reactions, being exothermic, yield additional heat that can and should be applied to assist with creating the conditions needed for these reactions to proceed most efficiently. As shown, the heat exchanger arrangement is in the form of a simple shell-and-tube heat exchanger, consisting of two concentric pipes: the inner forms the "tube", the outer, the "shell". An advantage with this arrangement is that the heat exchanger can be made as long as is required to effect the desired transfer of heat: if necessary, many hundreds of metres long. For heat exchanger 40 (i.e. the heat exchanger on the mine site side), heat energy is transferred between the final carbonate/silica product (i.e. slurry A), which is hot, and the silicate slurry (slurry B), which is cool. For heat exchanger 46 (i.e. the heat exchanger on the power station side), slurry A would be hot silicate slurry from the mine, while slurry B would be slurry exiting the scrubbing chamber 30 (i.e. now charged with ammonia and carbon dioxide, but at close to ambient temperatures).\|[0064] Turning now to Fig. 5, there is shown an alternative system 200 for performing carbon dioxide sequestration which utilises (where geological conditions permit) an underground chamber as the reactor, as opposed to a pipeline reactor as illustrated in Fig. 1. In this embodiment, the reactor is in the form of a chamber 70 excavated from bedrock at a depth sufficient to allow the conditions for the core carbonation reactions to be generated entirely or partly by static head alone (e.g. 120 Bar for the carbonation reactions and 20 Bar for the recovery of ammonia gas from the reaction products). A chamber 70 excavated at a depth of approximately 1,000 meters and having a volume of 150,000 cubic meters, sufficient to allow for a 24 hours detention time for the contents, may be envisaged for holding the reactive slurry output from a system 200 fitted to an efficient 1,000MWe coal-fired power station. In practice a smaller chamber may suffice, should it arise that the reactions are essentially completed in less time.\|[0065] The silicate slurry 36 may be prepared either at the serpentine mine site and pumped overland to the power station site, or, the mineral could be railed, trucked or otherwise suitably transported to the power station site, and prepared there. Were the former course of action adopted, pipeline arrangements 44 would be considerably simpler than for the pipeline reactor embodiment described above with reference to Fig. 1. Specifically, the silicate slurry 36 would not be required to collect and transport heat and pressure energy from the mine site to the power station site, nor to host any residual ammonia. The pipeline 44 would simply be utilised for ore transport; whether it was transported as a lump product by rail or as slurry by pipeline would be determined mainly by economic considerations. It will be appreciated that in this embodiment, silicate slurry density could be substantially higher (e.g. 60 per cent solids), thereby reducing the volumes of silicate slurry required to be pumped, and allowing a lower pipeline velocity because of the reduced tendency for the solids in denser slurries to segregate and silt up the pipeline 44. Also, arrangements for conserving heat and pressure are much simpler than they would need to be for the pipeline reactor alternative.\|[0066] In Fig. 5, an injection pump 72 is utilised to drive the circulation of the reactive slurry from the scrubbing chamber 40, through a plurality of counter-current heat exchangers 74, 76, underground reactor 70 and ammonia gas recovery vessel 78 (flash/rectifying vessel) and back to the surface. It is envisaged that a formation of bubbles of ammonia gas may occur as the reacted slurry rises from the underground reactor 70 (a rise accompanied by a loss of static head, hence of pressure), thereby reducing the bulk density of the reacted slurry rising from the reactor. It follows that the required circulation could be achieved by entirely natural means: after the injection pump 72 has achieved the circulation necessary for the reaction to proceed, it may be taken off line. The design of injection pump 72 may be such that it could run backwards, that is to generate power, should the natural rate of circulation created by the buoyancy effect of ammonia bubbles forming in the reactor outlet pipe 80 be sufficiently strong.\|[0067] Heat exchangers 74, 76 are shown in schematic form at two locations on Fig. 5. In practice, the heat exchangers 74, 76 could be long, shell-and-tube designs, as shown in Fig. 4: they would span most of the vertical distance from the scrubbing chamber 40 down to the underground chamber 70. This is to say, whereas two separate pipelines are implied in Fig. 5, in practice, for most of their length they would be concentric: the annulus formed between the outer and concentric inner pipe would transport the hot reaction products, while the inner pipe would transport the products heading downward to the Reaction chamber. It will be understood by persons skilled in the art that this selection may be reversed.\|[0068] In contrast to the pipeline reactor configuration shown in Fig. 1, heating of the reactive slurry is accomplished by exchanging heat from the hot reaction products rising first from the ammonia gas recovery vessel 78, and as the raw slurry descended further, from hot slurry rising from the underground chamber 70. While some supplementary heat may be required, the heat generated by Equation 2(b) would be conserved, and available to heat raw reactive slurry.\|[0069] The design of the underground chamber 70 may be optimised to achieve some plug-flow characteristics. In an embodiment, the chamber 70 may have a high length-to-diameter ratio and be vertically aligned. In this manner, the incoming reactive slurry, being cooler hence slightly denser than the average contents of the reactive chamber 70, would tend to stratify at lower levels, displacing hotter slurry upwards. In an embodiment, the underground chamber 70 may be subdivided into two or more vertically stacked sub-chambers.\|[0070] There should be no requirement for separate agitation equipment in the reaction chamber to maintain the solids in suspension. As shown in Fig. 5, incoming reactive slurry enters the vessel close to its base, and it is envisaged that settling rates will be small relative to overall slurry up-flow rates. If, however, large residence times are required, implying in turn large reactor volumes, a form of agitation may be implemented.\|[0071] As will readily be appreciated, heat losses from the underground chamber 70 and pipelines may be much smaller than they would be even from a lagged above-ground pipeline and may be further reduced by insulation surrounding the reactor, pipelines and all other underground process vessels. Whereas an overland pipeline represents a plug-flow reactor, ideal conditions for a relatively slow series of reactions as are involved in carbon sequestration are also obtained in the embodiment illustrated in Fig. 5.\|[0072] Also in Fig. 5, an alternative ammonia absorption recovery process is utilised. In this embodiment, as the final product slurry rises from the underground chamber 70, the static head it experiences may decrease. A consequence of this is that the boiling point temperature will fall, eventually below that of the slurry rising in the products pipeline, leading to the flashing of some of the water to steam, and the stripping of ammonia from solution. As ammonia comes out of the solution as a gas it will absorb latent heat from the final product slurry, partially cooling it; the temperature would tend to track the boiling point of water at the prevailing pressure. The bubbles of ammonia will reduce the average density of slurry in the hot products pipeline to below that in the incoming reactants pipeline, leading to a pressure differential in the system that would serve to drive the circulation of the reactant and product slurries from the CO2 Absorber 30 and through the underground chamber 70, heat exchangers and other items of process plant. As shown on Fig. 5, the ammonia recovery vessel 78 and other necessary plant and equipment for recovering ammonia from the product slurries are installed at a level (perhaps 150 metres below ground level) that facilitate the use of static head to maintain a pressure in the vessel 78 of around 15 Bar, i.e. high enough so that ammonia was a liquid at near-ambient temperatures.\|[0073] As for the pipeline reactor case, the ammonia will be discharged as a gas from the top of the vessel 78, however due to the circumstances outlined above, this vessel 78 could be much simpler in design and, in an embodiment, need be little more than a gas-liquid separator. While some additional heat energy may be required to recover essentially all of the ammonia as a gas, typically as steam, with the arrangements proposed the heat-energy burden of carbon sequestration could be greatly reduced.\|Examples\|[0074] Again with specific reference to Fig. 2, a non-limiting example process flow for carbon sequestration for the first system configuration 10 described herein (i.e. the system depicted in Fig. 1) will now be given, wherein for convenience, like parts to those shown in the foregoing embodiment have been numbered with like numerals.\|Example 1\|[0075] Table 1: Indicative mass and heat balance figures from 1.000 MWe of black coal-fired electricity generation plant.MaterialPer yearPer hourTotal CO2 generated:6.4 106 t800 tSilicate rock to absorb 90% of this CO2:145m 106 t1,800 tWater required to make 30% by wt slurry:33.6 106 t4,200Ammonia to conv. 90% of CO2 to (NH4)2CO3:4.45 106 t560 tHeat liberated (3.6 GJ/t CO2):2,800 GJTotal slurry with (NH4)2CO3:58 106 t7,2501Slurry density:1.3 t/m31.3 t/m3Slurry pipe dia. (both with 2 m/s velocity:1.0 m1.0 metresAmmonia pipe diameter, 2 m/s velocity0.4 m0.4 metresConc. of ammonia in Absorber aq. phase:12% (by wt)12%Ammonia lost due to SOx16,000 t2.0 tAmmonia lost due to NOx3,000 t0.37 tOther losses of ammonia:11,000 t1.38 tAmmonia make-up % of flow to Absorber:0.67%0.67%\|[0076] Table 1 provides a detailed mass and heat balance for a carbon dioxide sequestration process, assuming:\| 90 per cent carbon dioxide capture and sequestration from 1,000 MWe of black coal-fired electricity generation plant, which when operating in base-load mode might expect to generate annually 8,000 GWh of electricity;\| where on a dry ash-free basis, the coal is 81.3% by weight carbon and 0.65% sulphur (as S) and the flue gases contain 400 ppm NOx.\|[0077] The heat of formation of ammonium carbonate in solution from ammonia, water and carbon dioxide is around 2.0 GJ/tonne carbon dioxide equivalent, sufficient to heat the slurry by 75°C. Offsetting this is the heat absorbed when each tonne of ammonia is vaporised in the absorption zone, around 1.0 GJ/tonne ammonia. This is equivalent to around 1.8 GJ per tonne of carbon dioxide absorbed, sufficient to cool the slurry feed by around 60°C. It follows that there would be an overall temperature rise between the time the slurry feed enters the absorption zone and the time it enters the return pipeline 52, of around 15°C. In practice, it may be necessary to design the process so that the last slurry feed that the final largely carbon dioxide free flue gases is the coldest: less than 5°C.\|[0078] As well, the heat released when ammonium carbonate in solution reacts with the silicate rocks, roughly 1.45 GJ/tonne carbon dioxide absorbed, is sufficient to raise the temperature of the slurry feed by around 55°C. This occurs in the return pipeline 52.\|[0079] At the mine, the condensation of around 300 tonnes per hour of ammonia would release some 160 MWt of heat energy, which can be rejected to the environment via a cooling tower.\|[0080] An advantage of the carbon dioxide sequestration process 100 and systems 10, 20 according to embodiments of the present invention is that by selecting ammonia as a catalyst/promoter, a single integrated process can be provided for both capture and sequestration of carbon dioxide. In an embodiment, sequestration of the carbon dioxide takes place in a reactor, in the form of a return pathway 52 of a pipeline 44, which advantageously connects the power station (i.e. the source of carbon dioxide) to the source/destination of the absorbent material being used in the process. In an alternative embodiment, where geological conditions permit, the reactor may take the form of an underground chamber which advantageously facilitates the reaction without requiring pressure-exchange and head-recovery equipment required for the pipeline embodiment. Another advantage of the carbon dioxide sequestration process and systems is that the reaction kinetics may be improved by using ammonia. Therefore, by using ammonia and exploiting the heat generated by the exothermic reaction, the energy consumption of the process 100 can be kept to a minimum. As the reaction products are thermodynamically stable, carbon dioxide can be stored in a permanent stable solid form. Following from this, further advantages include lower operating and capital costs.\|[0081] Persons skilled in the art will appreciate that further advantages may arise from carrying out certain steps of the aforementioned embodiments in isolation. For example, the catalytic effect of a solution of ammonia with an ammonium salt (that may be ammonium carbonate formed by exposing an ammonia-rich solution to a gas stream containing carbon dioxide) in the carbon dioxide sequestration process can also be utilised for extracting metals (e.g. magnesium, iron, nickel, copper and other metals present in the silicate rock) from metal silicates, such as magnesium-rich metal silicates. In such an embodiment a solution comprising ammonia and ammonium may be mixed with a metal silicate (typically in slurry form) to allow the dissolution of magnesium ions by ammonia to recover the metal, in this embodiment a metal compound in the form of magnesium carbonate. The mixing may occur in an ammonia absorption chamber such as that previously described in connection with the preceding embodiments. Preferably the ammonia solution comprises concentrated ammonia in the presence of ammonia salts in solution, such as ammonium carbonate, to prevent the precipitation of magnesium hydroxide, hence allowing the dissolution of magnesium ions by ammonia to continue. A further advantage arising from this process is that after extraction of magnesium carbonate, other minerals (metals) present within the silicate rock are also amenable to recovery. The silicate rock may comprise mafic or ultra-mafic rocks (i.e. rocks with a high magnesium content).\|[0082] The catalytic effect of the ammonia follows from its tendency to form complexes (ammines) with certain metal ions including magnesium (Mg2+), divalent iron (Fe2+), copper (Cu2+) and nickel (Ni2+). The presence of ammonium salts notably the carbonate formed from the reaction between ammonia and carbon dioxide prevents precipitation of the otherwise insoluble magnesium hydroxide. Magnesium carbonate is however insoluble in such an environment, so a precipitate of this compound will form from the reaction between magnesium hydroxide and ammonium carbonate, to yield ammonium hydroxide and free ammonia in solution, the latter continuing to extract additional magnesium and other metals from the silicate rock through formation of ammine complexes until all such susceptible metals have been extracted.\|[0083] Subsequently, the ammonia is recovered from the solution by in the ammonia recovery vessel, a consequence being a progressive reduction in the concentration of free ammonia in the reactive slurry. This leads to destruction of the metal ammine complexes, but in a progressive manner, depending on the stability of the complexes, which stability in turn differs between metals. Those of magnesium are relatively weak (the reason most of the magnesium will have precipitated out as magnesium carbonate), so the first salt to be precipitated is further magnesium carbonate. As the concentration of ammonia in solution continues to fall, other metals can precipitate in sequence, allowing the opportunity of obtaining precipitates of each single metal in relatively pure form.\|[0084] Finally, it is to be appreciated that various alterations or additions may be made to the parts previously described without-departing from the spirit or ambit of the present invention as defined by the following claims. The process is not limited to having a single two-stage continuous reactor, or a single tube-like reactor, as the process may be arranged to utilise alternatively configured items of equipment as necessary to accommodate process variables, arising from different source materials, capital and operating costs. For example, in the exemplary embodiment previously described the plant design is based on the emission of 800 tonnes CO2/GWh generated from a state-of-the-art black coal-fired electricity generation plant. By comparison, the Bayswater Power Station and the Liddell Power Station, both in the Hunter Valley of New South Wales, Australia, able to generate 2,640 MWe and 2,040 MWe respectively, being older hence less efficient can be expected to emit between 850 and 900 tonnes CO2/GWh.\|[0085] Thus the concentration and rate of carbon dioxide emissions in the flue gas emitted by the power plant may vary such that the plant equipment design may be reconfigured to accommodate these variables. For example, alternative equipment can be configured for the various heat and pressure exchange stations. The carbon dioxide absorption zone and the scrubbing zone may be arranged in series in two separate vessels (rather than the nested configuration shown in Fig. 1). The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s). As well, the corresponding solids concentration in the slurry feed may be higher or lower than 30% solids by weight. It is possible that the metal silicate solution may comprise a blend of metal silicates, e.g. mixture of serpentines and olivines, even pyroxenes. The reaction kinetics may require heat to be removed from the reactive solution (rather than heat addition as described above). These factors will impact and alter the system pressures. There might be two or more pipelines for transporting the metal silicate solution and the reactive solution; because there are more pipelines additional heat exchangers and pressure-exchange apparatus may be used. The power station flue gas may include additional pre-processing steps including flue gas desulphurisation (FGD) and selective catalytic reduction (SCR) to reduce concentrations of SOx and NOx respectively hence losses of ammonia from the system. Furthermore, the availability of services, such as steam and cooling water may require different equipment arrangements.\|[0086] Any reference to prior art contained herein is not to be taken as an admission that the information is common general knowledge, unless otherwise indicated.\|[0087] In the claims which follow and in the preceding description of the invention, except where the context requires otherwise due to express language or necessary implication, the word "comprise" or variations such as "comprises" or "comprising" is used in an inclusive sense, i.e. to specify the presence of the stated features but not to preclude the presence or addition of further features in various embodiments of the invention.	Family Number\|(6597398)\|6597398\|Object of Invention\|(AU2008217572 B2)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|In accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|(AU2009250983 A1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|In accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|(CA2678800 C)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(CA2678800 A1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(CN101641145B B)\|A first aspect of the invention provides a method of carbon dioxide sequestration , the method comprising the steps of : \|The present invention relates generally to systems , apparatus and methods for carbon dioxide sequestration and more particularly , but not exclusively , to systems and methods for the capture and sequestration of carbon dioxide from power plant flue gases . \|The present invention relates to a method for carbon dioxide sequestration comprising the following steps . \|(CN101641145 A)\|A first aspect of the invention provides a method of carbon dioxide sequestration , the method comprising the steps of : \|The present invention relates generally to systems , apparatus and methods for carbon dioxide sequestration and more particularly , but not exclusively , to systems and methods for the capture and sequestration of carbon dioxide from power plant flue gases . \|The present invention relates to a method for carbon dioxide sequestration comprising the following steps . \|(EP2134449 B1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with (...) \|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(JP5345954 B2)\|The present invention relates generally to systems, apparatuses, and methods for carbon dioxide isolation, and more particularly to (but not limited to) systems and methods for capturing and isolating carbon dioxide from power plant flue gases.\|(JP2010519027 A)\|The present invention relates generally to systems, apparatuses, and methods for carbon dioxide isolation, and more particularly to (but not limited to) systems and methods for capturing and isolating carbon dioxide from power plant flue gases.\|(KR101527365 B1)\|A first aspect of the present invention is a process for producing ammonia/water/metal silicate slurry, the process comprising the steps of: (i) mixing ammonia with a slurry of metal silicate rock to produce an ammonia/water/metal silicate slurry; (ii) scrubbing a carbon dioxide-containing gas stream with the solution obtained from the first step (i), A second step of absorbing carbon dioxide into the reactive slurry; and (iii) a third (...) \|The present invention relates to systems, apparatuses and methods for carbon dioxide isolation, and more particularly, but not exclusively, to apparatuses and methods for capturing and isolating carbon dioxide from power plant flue gases.\|(KR20090125109 A)\|A first aspect of the present invention is a process for producing ammonia/water/metal silicate slurry, the process comprising the steps of: (i) mixing ammonia with a slurry of metal silicate rock to produce an ammonia/water/metal silicate slurry; (ii) scrubbing a carbon dioxide-containing gas stream with the solution obtained from the first step (i), A second step of absorbing carbon dioxide into the reactive slurry; and (iii) a third (...) \|The present invention relates to systems, apparatuses and methods for carbon dioxide isolation, and more particularly, but not exclusively, to apparatuses and methods for capturing and isolating carbon dioxide from power plant flue gases.\|(US8496897 B2)\| (...) This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|(US20100021362 A1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(WO2008101293 A1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(IN-293376 B)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(IN2009DN06026 A)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. (...) \|Abstract\|(AU2008217572 B2)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From US8496897 B2)\|(AU2009250983 A1)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From US8496897 B2)\|(CA2678800 C)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|(CN101641145B B)\|A carbon dioxide sequestration process includes the following steps . In a first stage , a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia / water / metal silicate slurry . In a second stage , the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry . In a third stage , the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate . \|(EP2134449 B1)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|(KR101527365 B1)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.COPYRIGHT KIPO & WIPO 2010\|(US8496897 B2)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|(WO2008101293 A1)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|(IN-293376 B)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|Title\|(AU2008217572 B2)\|System, apparatus and method for carbon dioxide sequestration\|(AU2008217572 A1)\|System, apparatus and method for carbon dioxide sequestration\|(AU2009250983 A1)\|System, apparatus and method for carbon dioxide sequestration\|(CA2678800 C)\|System, apparatus and method for carbon dioxide sequestration\|(CA2678800 A1)\|System, apparatus and method for carbon dioxide sequestration\|(CN101641145B B)\|System , apparatus and method for carbon dioxide sequestration \|(CN101641145 A)\|System , apparatus and method for carbon dioxide sequestration \|(EP2134449 B1)\|System, apparatus and method for carbon dioxide sequestration\|(EP2134449 A4)\|System, apparatus and method for carbon dioxide sequestration\|(EP2134449 A1)\|System, apparatus and method for carbon dioxide sequestration\|(KR101527365 B1)\|System, apparatus and method for carbon dioxide sequestration\|(KR20090125109 A)\|System, apparatus and method for carbon dioxide sequestration\|(US8496897 B2)\|System, apparatus and method for carbon dioxide sequestration\|(US20100021362 A1)\|System, apparatus and method for carbon dioxide sequestration\|(WO2008101293 A1)\|System, apparatus and method for carbon dioxide sequestration\|(IN-293376 B)\|System, apparatus and method for carbon dioxide sequestration\|(IN2009DN06026 A)\|System, apparatus and method for carbon dioxide sequestration\|Advantages / Prev. Drawbacks\|(AU2008217572 B2)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(AU2009250983 A1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(CA2678800 C)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(CA2678800 A1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(CN101641145B B)\|The inventors have found that the use of ammonia as catalyst has particular advantages : it can be used both for separating carbon dioxide from a gas mixture ( called carbon capture ) and for its permanent isolation in a single integrated process . \|(CN101641145 A)\|The inventors have found that the use of ammonia as catalyst has particular advantages : it can be used both for separating carbon dioxide from a gas mixture ( called carbon capture ) and for its permanent isolation in a single integrated process . \|(EP2134449 B1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(US8496897 B2)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(US20100021362 A1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(WO2008101293 A1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(IN-293376 B)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|Independent Claims\|(AU2008217572 B2)\|1. A carbon dioxide sequestration process including the steps of:(i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (...) \|27. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|(AU2009250983 A1)\|1. A carbon dioxide sequestration process including the steps of:(i) in a fast stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (...) \|27. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|33. In an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, the steps of: (...) \|(CA2678800 C)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the ammonia/water/metal silicate slurry from (i) to thereby absorb the carbon dioxide into a (...) \|(CA2678800 A1)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the ammonia/water/metal silicate slurry from (i) to thereby absorb the carbon dioxide into a (...) \|(CN101641145B B)\|1. A method of carbon dioxide sequestration , the method comprising the steps of : ( i ) in a first stage , mixing a slurry of metal silicate rock with ammonia to produce an ammonia / water / metal silicate slurry ; ( . . . ) \|(CN101641145 A)\|1. A method of carbon dioxide sequestration , the method comprising the steps of : ( i ) in a first stage , mixing a slurry of metal silicate rock with ammonia to produce an ammonia / water / metal silicate slurry ; ( . . . ) \|27. In a pipeline , providing a first flow path with a metal silicate slurry for use by a first apparatus in a carbon sequestration process ; and a second flow path with the reactive slurry from the first apparatus and comprising carbon dioxide absorbed in the ammonia / water / metal silicate slurry , wherein the second flow path is controlled to promote the reaction of carbon ( . . . ) \|33. In an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia to produce an ammonia / water / metal silicate slurry for use in a carbon dioxide sequestration process , the following steps are provided : ( . . . ) \|(EP2134449 B1)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) (...) \|(KR101527365 B1)\|1. A method of carbon dioxide sequestration comprising: (i) A method for producing a metal silicate, comprising: a first step of mixing a slurry of metal silicate rock with ammonia to produce a slurry composed of ammonia/water/metal silicate; (ii) A second step of scrubbing the carbon dioxide (...) controlled in order to promote the reaction between carbon dioxide and the metal silicate and to produce metal carbonate, Carbon dioxide sequestration method.\|(KR20090125109 A)\|1. A method of carbon dioxide sequestration comprising: (i) A first step of mixing ammonia with a slurry of metal silicate rock to produce an ammonia/water/metal silicate slurry; (ii) A second step of scrubbing the carbon dioxide containing gas flow (...) controlled reactor in order to promote the reaction between carbon dioxide and the metal silicate and produce metal carbonate, Carbon dioxide sequestration method.\|27. A pipeline, comprising: A first flow path carrying metal silicate for use by a first device in a carbon sequestration process; and A second flow path carrying the reactive slurry from the first device and comprising carbon dioxide absorbed in the ammonia/water/metal silicate slurry, Wherein the second flow path is controlled to cause carbon dioxide to react (...) \|33. An ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia to produce ammonia/water/metal silicate for use in a carbon dioxide sequestration process, (i) Bringing ammonia into pressurized liquid form to expand in an evaporator stage to provide a cooling effect in said evaporator stage prior to passing it through an absorption process; and (ii) Passing the ammonia/water/metal silicate (...) \|(US8496897 B2)\|1. A carbon dioxide sequestration process including the steps of: (i) providing a slurry comprising metal silicate rock; (ii) in a first stage, mixing the slurry of metal silicate rock with ammonia so as to produce an ammonia/water/metal silicate slurry; (iii) in a second stage, scrubbing a gas stream containing carbon dioxide with the slurry from (ii) to thereby absorb the carbon dioxide into the slurry so as to form a reactive (...) \|18. An ammonia absorption process in a carbon dioxide sequestration process, the ammonia absorption process comprising the steps of: (i) producing a slurry of metal silicate rock mixed with ammonia so as to produce an ammonia/water/metal silicate slurry; (ii) provide pressurized ammonia in liquid form; (iii) expanding the pressurized ammonia in liquid form in an evaporator stage so as to provide a cooling effect in (...) \|(US20100021362 A1)\| (...) A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) (...) \| (...) In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \| (...) In an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, the steps of: (i) prior to passing the ammonia to the absorption process, allowing the ammonia in pressurised liquid form to expand in an evaporator stage so as to provide a cooling effect in that stage; and (ii) passing the ammonia/water/metal (...) \|(WO2008101293 A1)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) (...) \|27. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|33. In an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, the steps of: (i) prior to passing the ammonia to the absorption process, allowing the ammonia in pressurised liquid form to expand in an evaporator stage so as to provide a cooling effect in that stage; and (ii) passing the ammonia/water/metal (...) \|(IN-293376 B)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) (...) \|	Environmental technology\|Materials, 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CAT=102\|JP5345954 6597398 WHO=Examiner SELF=N\|WO200608242 62088431 WHO=Applicant SELF=N\|WO200608242 62088431 WHO=Applicant SELF=N\|WO200608242 62088431 WHO=Applicant SELF=N\|WO200608242 62088431 WHO=Examiner SELF=N\|WO200608242 62088431 WHO=Examiner SELF=N\|WO2005108297 43690578 WHO=Applicant SELF=N\|WO2005108297 43690578 WHO=Applicant SELF=N\|WO2005108297 43690578 WHO=Applicant SELF=N\|WO2005108297 43690578 WHO=Examiner SELF=N\|WO2005108297 43690578 WHO=Examiner SELF=N\|WO200622885 76566186 WHO=Applicant SELF=N\|WO200622885 76566186 WHO=Applicant SELF=N\|WO200498740 43663450 WHO=Applicant SELF=N\|WO200498740 43663450 WHO=Applicant SELF=N\|WO200498740 43663450 WHO=Applicant SELF=N\|WO200498740 43663450 WHO=Examiner SELF=N\|WO200498740 43663450 WHO=Examiner SELF=N\|WO200494043 1759232 WHO=Applicant SELF=N\|WO200494043 1759232 WHO=Applicant SELF=N\|WO200494043 1759232 WHO=Applicant SELF=N\|WO200494043 1759232 WHO=Examiner SELF=N\|WO200494043 1759232 WHO=Examiner SELF=N\|JP2005097072 22202253 WHO=Applicant SELF=N\|JP2005097072 22202253 WHO=Examiner SELF=N\|JP2005097072 22202253 WHO=Examiner SELF=N\|CN1106311 4817315 WHO=Applicant SELF=N\|CN1106311 4817315 WHO=Examiner SELF=N\|US4226277 59919407 WHO=Examiner SELF=N\|US2829060 41539758 WHO=Examiner SELF=N	W. K. O, CONNOR, ET AL: "Carbon dioxide sequestration by direct mineral carbonation : process mineralogy of feed and products", 《 2001SME ANNUAL MEETING&EXHIBIT》 (Cat. X)\|S.J.Gerdemann et al..THE GRAVITY-PRESSURIZED REACTOR AS A MEANS TO EFFICIENTLY CARRY OUT METALLURGICALLY IMPORTANT REACTIONS.《chemical engineering science》.1992,第47卷(第13/14期),3753-3760.\|特開2005−097072(JP,A)\|国際公開第2004/094043(WO,A1)	WO200608242; WO2005108297; WO200498740; WO200494043; WO200608242; WO200494043; WO2005108297; WO200498740; WO200622885\|\|\|\|JP2005097072; JP5345954\|WO200498740; WO200608242; WO200494043; CN1106311; WO2004098740; WO2005108297; WO2006008242; WO2004094043\|JP2005097072; WO200494043\|US4226277; US2829060; US4308241; WO200608242; CN1106311; JP2005097072; WO200494043; WO200498740; WO2005108297; WO200608242\|WO200608242; WO2005108297; WO200498740; WO200494043; XP002619884; WO200608242; WO200494043; WO2005108297; WO200498740; WO200622885\|WO2005108297; WO200608242; WO200498740	(EP2134449)\|Search Report references [Examiner]\|-See also references of WO 2008101293A1\|-GERDEMANN S J ET AL: "Gravity-pressurized reactor as a means to efficiently carry out metallurgically important reactions", CHEMICAL ENGINEERING SCIENCE 1992 SEP-OCT,, vol. 47, no. 13-14, 1 September 1992 (1992-09-01), pages 3753 - 3760, XP002619884\|\|(US8496897)\|Pre-Search references [Examiner]\|-Sugiyama, "Phase Diagram." 8/24/2002. Downloaded 12/17/09 from http://www.gfd-dennou.org/library/oboro/gallery/output/phase/index.html.en .\|-Fauth et al., "Carbon dioxide storage as mineral carbonates." ACS Div. of Fuel Chem. Preprints, Vol. 45, Issue 4, 2000 (no month), pp. 708-712.\|-Ophardt, Charles E., "Virtual Chembook." Elmhurst College (2003). Viewed 8/12/12 at http://www.elmhurst.edu/~chm/vchembook/174temppres.html .\|-Simtronics Corp., "SPM-3100 Amine Treating Unit." Published 2006. Viewed 8/12/12 at http://www.simtronics.com/catalog/spm/spm3100.htm .\|-English translation of second office action issued Apr. 5, 2012 by State Intellectual Property Office of P.R. China for corresponding Chinese application 200880006610.5.\|-Sugiyama, "Phase Diagram." Aug. 24, 2002. Downloaded Dec. 17, 2009 from http://www.gfd-dennou.org/library/oboro/gallery/output/phase/index.html.en.\|-Fauth et al., "Carbon dioxide storage as mineral carbonates." ACS Div. of Fuel Chem. Preprints, vol. 45, Issue 4, 2000 (no month), pp. 708-712.\|-Ophardt, Charles E., "Virtual Chembook." Elmhurst College (2003). Viewed Aug. 12, 2012 at http://www.elmhurst.edu/~chm/vchembook/174temppres.html.\|-Simtronics Corp., "SPM-3100 Amine Treating Unit." Published 2006. Viewed Aug. 12, 2012 at http://www.simtronics.com/catalog/spm/spm3100.htm.\|\|(WO2008/101293)\|Applicant references\|-See also references of EP 2134449A4\|\|\|\|\|\|\|\|	GRANTED	(EP2134449)\|LAPSED\|(US8496897)\|LAPSED\|(WO2008/101293)\|LAPSED\|(JP5345954)\|LAPSED\|(CN101641145)\|LAPSED\|(IN293376)\|GRANTED\|(CA2678800)\|LAPSED\|(KR10-1527365)\|LAPSED\|(AU2008217572)\|EXPIRED\|(AU2009250983)\|LAPSED	ALIVE	(EP2134449)\|DEAD\|(US8496897)\|DEAD\|(WO2008/101293)\|DEAD\|(JP5345954)\|DEAD\|(CN101641145)\|DEAD\|(IN293376)\|ALIVE\|(CA2678800)\|DEAD\|(KR10-1527365)\|DEAD\|(AU2008217572)\|DEAD\|(AU2009250983)\|DEAD	(EP2134449)\|LEGAL DETAILS FOR EP2134449\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP08706115\|Application date=2008-02-20\|Standardized application number=2008EP-0706115\|Event publication date=2009-11-20\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2009-12-23\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2134449\|Publication stage code=A1\|Publication date=2009-12-23\|Standardized publication number=EP2134449\|Event publication date=2009-12-23\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2009-09-17\|Event publication date=2009-12-23\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR\|Event publication date=2010-05-26\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2011-03-30\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP2134449\|Publication stage code=A4\|Publication date=2011-03-30\|Standardized publication number=EP2134449\|Event publication date=2011-03-30\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2011-02-25\|Event publication date=2011-11-09\|Event code=EP/17Q\|Event indicator=Pos\|Event group=Examination events\|First examination report\|Erster pruefungsbescheid\|Effective date of the event=2011-10-11\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-25\|Event code=EP/GRAP\|Event indicator=Pos\|Event group=Examination events\|DESPATCH OF COMMUNICATION OF INTENTION TO GRANT A PATENT\|New entry: communication of intention to grant a patent\|Original code: EPIDOSNIGR1\|Event publication date=2012-08-31\|Event code=EP/GRAS\|Event indicator=Pos\|Event group=Examination events Payment or non-payment notifications\|GRANT FEE PAID\|New entry: payment of fee for grant\|Original code: EPIDOSNIGR3\|Event publication date=2012-09-07\|Event code=EP/GRAA\|Event indicator=Pos\|Event group=Examination events\|(EXPECTED) GRANT\|Original code: 0009210\|Event publication date=2012-10-10\|Event code=EP/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent specification\|Publication country=EP\|Publication number=EP2134449\|Publication stage code=B1\|Publication date=2012-10-10\|Standardized publication number=EP2134449\|Event publication date=2012-10-10\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR\|Event publication date=2013-08-16\|Event code=EP/PLBE\|Event indicator=Pos\|Event group=No opposition filed\|NO OPPOSITION FILED WITHIN TIME LIMIT\|Original code: 0009261\|Event publication date=2013-08-16\|Event code=EP/STAANOPP\|Event indicator=Pos\|Event group=No opposition filed Event indicating In Force\|No opposition filed within time limit\|Original code: STAA\|Event publication date=2013-09-18\|Event code=EP/26N\|Event indicator=Pos\|Event group=No opposition filed Event indicating In Force\|No opposition filed\|Kein einspruch eingelegt\|Effective date of the event=2013-07-11\|Event publication date=2018-10-31\|Event code=EP/LAPS\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Lapse of the protection rights for all corresponding member states\|EP lapsed due to lapse of contracting member states AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR\|Event publication date=2018-10-31\|Event code=EP/EXSN\|Notification: EP extension states status not included in change to EP status\|MEMBER STATE LEGAL DETAILS FOR AT\|Actual or expected expiration date=2012-10-10\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=AT Corresponding appl: AT578891\|Event publication date=2012-10-15\|Event code=EP/REG\|Event code=AT/REF\|Event indicator=Pos\|Event group=Entry into national phase\|Reference to a national code\|Reference to at number (ep patent enters austrian national phase)\|Nennung der e-nummer (EP patent tritt in at nationale phase ein)\|Effective date of the event=2012-10-15\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2013-03-15\|Event code=EP/REG\|Event code=AT/MK05\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Revocation of the translation of the ep patent\|Loeschung gemaess par. 5 (zurueckziehung der uebersetzung des ep patents)\|Effective date of the event=2012-10-10\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2013-06-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=AT\|MEMBER STATE LEGAL DETAILS FOR BE\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BE\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=BE\|MEMBER STATE LEGAL DETAILS FOR BG\|Actual or expected expiration date=2013-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BG\|Event publication date=2013-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=BG\|MEMBER STATE LEGAL DETAILS FOR CH\|Actual or expected expiration date=2013-09-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2012-10-15\|Event code=EP/REG\|Event code=CH/EP\|Event indicator=Pos\|Event group=Entry into national phase\|Reference to a national code\|EUROPEAN PATENT TAKES EFFECT AS A NATIONAL PATENT IN CH/LI\|Wirkung des europäischen patents als nationales patent in ch/li tritt ein\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2013-09-30\|Event code=EP/REG\|Event code=CH/PL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent ceased\|Loeschung/radiation/radiazion\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2013-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=CH\|MEMBER STATE LEGAL DETAILS FOR CY\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CY\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=CY\|MEMBER STATE LEGAL DETAILS FOR CZ\|Actual or expected expiration date=2013-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CZ\|Event publication date=2013-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=CZ\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2018-09-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE Corresponding appl: DE602008019269\|Event publication date=2012-03-12\|Event code=EP/REG\|Event code=DE/R079\|Event group=Corrections\|Reference to a national code\|Amendment of ipc main class\|Aenderung der IPC hauptklasse\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2012-03-12\|Event code=EP/REG\|Event code=DE/R079\|Event group=Corrections\|Reference to a national code\|Amendment of ipc main class\|Aenderung der IPC hauptklasse\|Previous main class: B01D0053620000\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2012-12-06\|Event code=EP/REG\|Event code=DE/R096\|Event indicator=Pos\|Event group=Examination events\|Reference to a national code\|DPMA publication of mentioned EP patent grant\|Veroeffentlichung eines hinweises auf die ep-patenterteilung durch das dpma\|Effective date of the event=2012-12-06\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2013-10-31\|Event code=EP/REG\|Event code=DE/R097\|Event indicator=Pos\|Event group=No opposition filed\|Reference to a national code\|No opposition filed against granted patent, or EPO opposition proceedings concluded without decision\|Gegen die patenterteilung wurde kein einspruch erhoben, bzw. einspruchsverfahren ist beim epa ohne entscheidung abgeschlossen\|Effective date of the event=2013-07-11\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2017-02-17\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2017-02-17\|Year of payment of annual fees=10\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-09-01\|Event code=EP/REG\|Event code=DE/R119\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Application deemed withdrawn, or ip right lapsed, due to non-payment of renewal fee\|Die anmeldung gilt als zurueckgenommen wegen nichtzahlung der jahresgebuehr / schutzrecht ist wegen nichtzahlung der jahresgebuehr verfallen\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR DK\|Actual or expected expiration date=2013-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DK\|Event publication date=2013-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=DK\|MEMBER STATE LEGAL DETAILS FOR EE\|Actual or expected expiration date=2013-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EE\|Event publication date=2013-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=EE\|MEMBER STATE LEGAL DETAILS FOR ES\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=ES\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=ES\|MEMBER STATE LEGAL DETAILS FOR FI\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=FI\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=FI\|MEMBER STATE LEGAL DETAILS FOR FR\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2016-01-25\|Event code=EP/REG\|Event code=FR/PLFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications Restitution or restoration\|Reference to a national code\|Fee payment\|Derniere annuite payee\|Annual fees payment date=2016-01-25\|Year of payment of annual fees=9\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2017-02-17\|Event code=EP/REG\|Event code=FR/PLFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications Restitution or restoration\|Reference to a national code\|Fee payment\|Derniere annuite payee\|Annual fees payment date=2017-02-17\|Year of payment of annual fees=10\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2017-02-17\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2017-02-17\|Year of payment of annual fees=10\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2018-11-30\|Event code=EP/REG\|Event code=FR/ST\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Notification of lapse\|Constatation de decheances\|Effective date of the event=2018-10-31\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2019-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=FR\|MEMBER STATE LEGAL DETAILS FOR GB\|Actual or expected expiration date=2018-02-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2012-10-10\|Event code=EP/REG\|Event code=GB/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patent granted\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2017-02-16\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2017-02-16\|Year of payment of annual fees=10\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2018-02-20\|Event code=EP/GBPC\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|GB: European patent ceased through non-payment of renewal fee\|Effective date of the event=2018-02-20\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2019-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=GB\|MEMBER STATE LEGAL DETAILS FOR GR\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GR\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=GR\|MEMBER STATE LEGAL DETAILS FOR HR\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=HR\|MEMBER STATE LEGAL DETAILS FOR HU\|Actual or expected expiration date=2015-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HU\|Event publication date=2015-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO\|Corresponding cc:\|Designated or member state=HU\|MEMBER STATE LEGAL DETAILS FOR IE\|Actual or expected expiration date=2013-12-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2012-11-07\|Event code=EP/REG\|Event code=IE/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patents granted designating Ireland\|European patent granted\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2013-12-04\|Event code=EP/REG\|Event code=IE/MM4A\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent lapsed\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2014-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=IE\|MEMBER STATE LEGAL DETAILS FOR IS\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IS\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IS\|MEMBER STATE LEGAL DETAILS FOR IT\|Actual or expected expiration date=2013-08-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2013-08-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IT\|MEMBER STATE LEGAL DETAILS FOR LI\|Actual or expected expiration date=2013-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LI\|Event publication date=2013-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LI\|MEMBER STATE LEGAL DETAILS FOR LT\|Actual or expected expiration date=2013-03-25\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2013-03-25\|Event code=EP/REG\|Event code=LT/MG4D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Invalidated european patent\|Europos patentai, laikomi ab initio negaliojanciais\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LT\|MEMBER STATE LEGAL DETAILS FOR LU\|Actual or expected expiration date=2015-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LU\|Event publication date=2015-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LU\|MEMBER STATE LEGAL DETAILS FOR LV\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LV\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LV\|MEMBER STATE LEGAL DETAILS FOR MC\|Actual or expected expiration date=2013-09-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MC\|Event publication date=2013-09-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=MC\|MEMBER STATE LEGAL DETAILS FOR MT\|Actual or expected expiration date=2014-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MT\|Event publication date=2014-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MT\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=2012-10-10\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2013-03-13\|Event code=EP/REG\|Event code=NL/VDEP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Invalid in the netherlands as no translation has been filed\|Verval wegens niet indienen vertaling\|Effective date of the event=2012-10-10\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NL\|MEMBER STATE LEGAL DETAILS FOR NO\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NO\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NO\|MEMBER STATE LEGAL DETAILS FOR PL\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PL\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PL\|MEMBER STATE LEGAL DETAILS FOR PT\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PT\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PT\|MEMBER STATE LEGAL DETAILS FOR RO\|Actual or expected expiration date=2013-08-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RO\|Event publication date=2013-08-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RO\|MEMBER STATE LEGAL DETAILS FOR SE\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SE\|MEMBER STATE LEGAL DETAILS FOR SI\|Actual or expected expiration date=2013-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SI\|Event publication date=2013-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SI\|MEMBER STATE LEGAL DETAILS FOR SK\|Actual or expected expiration date=2013-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SK\|Event publication date=2013-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SK\|MEMBER STATE LEGAL DETAILS FOR TR\|Actual or expected expiration date=2015-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=TR\|Event publication date=2015-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=TR\|(US8496897)\|LEGAL DETAILS FOR US8496897\|Actual or expected expiration date=2021-09-06\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US12527608\|Application date=2008-02-20\|Standardized application number=2008US-12527608\|Event publication date=2008-02-20\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:BERNS, DANIEL J\|Event publication date=2008-02-20\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2008-02-20\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 930125-2009\|Event publication date=2008-02-20\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 20999\|Event publication date=2008-02-20\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2008-02-20\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2009-08-18\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2009-08-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2009-10-16\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2009-10-16\|Event code=US/M903\|Event indicator=Pos\|Event group=Examination events OAO\|Notice of DO/EO Acceptance Mailed\|Event publication date=2009-12-14\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2010-01-28\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20100021362\|Publication stage code=A1\|Publication date=2010-01-28\|Standardized publication number=US20100021362\|Event publication date=2010-01-28\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2010-10-06\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-07-06\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-07-14\|Event code=US/RESTREQ\|Event group=Examination events Corrections OAO\|Restriction/Election Requirement\|Event publication date=2011-08-15\|Event code=US/ELC\|Event group=Examination events OAI\|Response to Election / Restriction Filed\|Event publication date=2011-11-10\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2011-11-29\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2011-11-29\|R4R=112\|RJST=non-final\|Rejected claims 1-20, 33-35 and 38; 33\|Event publication date=2011-11-29\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2011-11-29\|R4R=102b\|RJST=non-final\|Rejected claims 1 and 4\|RJCT=WO200608242\|Event publication date=2011-11-29\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2011-11-29\|R4R=103a\|RJST=non-final\|Rejected claims 1, 3-6, 11 and 16-19; 1-6, 11, 16-20, 33-35 and 38; 1, 3-6, 9-11 and 14-19\|Event publication date=2012-03-29\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2012-03-29\|Event code=US/136G\|Event group=OAO\|Request for Extension of Time - Granted\|Event publication date=2012-05-24\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-07-23\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-09-27\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2012-10-09\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2012-10-09\|R4R=112\|RJST=non-final\|Rejected claims 35\|Event publication date=2012-10-09\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2012-10-09\|R4R=102b\|RJST=non-final\|Rejected claims 38\|RJCT=WO200608242\|Event publication date=2012-10-09\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2012-10-09\|R4R=103a\|RJST=non-final\|Rejected claims 2 and 20; 3; 8; 9 and 10\|RJCT=US4308241\|Event publication date=2013-02-26\|Event code=US/136G\|Event group=OAO\|Request for Extension of Time - Granted\|Event publication date=2013-02-26\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Action Recorded:\|RECD=2013-02-26\|Event publication date=2013-05-21\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2013-05-21\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2013-05-29\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2013-06-17\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2013-06-17\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2013-06-24\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2013-07-10\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2013-07-30\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US08496897\|Publication stage code=B2\|Publication date=2013-07-30\|Standardized publication number=US8496897\|Event publication date=2013-07-30\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 655 Overlap Delays: 50 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 193 Adjustment total: \|Number of days of extension=412\|Event publication date=2013-07-30\|Event code=US/PTA36\|Event group=Extension of term of duration of protection\|PTA 36 Months\|Action Recorded:\|RECD=2013-07-30\|Event publication date=2016-08-09\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2017-01-16\|Event code=US/FPAY\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Fee payment recorded\|Annual fees payment date=2017-01-16\|Year of payment of annual fees=4\|Event publication date=2020-08-11\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|Event publication date=2021-03-22\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2021-07-30\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2021-07-30\|Event publication date=2021-09-06\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2021-09-06\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|Event publication date=2024-08-13\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=11\|(WO2008/101293)\|LEGAL DETAILS FOR WO2008/101293\|Actual or expected expiration date=2010-08-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOAU2008000232\|Application date=2008-02-20\|Standardized application number=2008WO-AU00232\|Event publication date=2008-08-28\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2008101293\|Publication stage code=A1\|Publication date=2008-08-28\|Standardized publication number=WO2008101293\|Event publication date=2010-11-22\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2008217572\|Actual or expected expiration date=2018-09-13\|Legal state=DEAD\|Status=EXPIRED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2008217572\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2008AU-0217572\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2008217572\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2008-08-28\|Publication number in the designated or member state=AU2008217572\|Event publication date=2009-09-18\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2009-10-15\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2018-09-13\|Event code=AU/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=AU\|MEMBER STATE LEGAL DETAILS FOR CA2678800\|Actual or expected expiration date=2019-02-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA2678800\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2008CA-2678800\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA2678800\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2008-08-28\|Publication number in the designated or member state=CA2678800\|Event publication date=2009-08-19\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CA\|Event publication date=2019-04-03\|Event code=CA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR CN101641145\|Actual or expected expiration date=2018-02-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN200880006610\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2008CN-80006610\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN101641145\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2010-02-03\|Publication number in the designated or member state=CN101641145\|Event publication date=2008-02-20\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CN\|Event publication date=2019-02-15\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2009-08-21\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2009-08-21\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP2134449\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP08706115\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2008EP-0706115\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2134449\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2009-12-23\|Publication number in the designated or member state=EP2134449\|Event publication date=2008-10-15\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2009-09-17\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2013-09-18\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR IN6026/DELNP/2009\|Actual or expected expiration date=2028-02-20\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN6026/DELNP/2009\|Application date in the designated or member state=2009-09-18\|Application number in the designated or member state=2009IN-DN06026\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN6026/DELNP/2009\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-08-26\|Publication number in the designated or member state=IN2009DN06026\|Event publication date=2009-09-18\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|Event publication date=2018-02-26\|Event code=IN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IN\|MEMBER STATE LEGAL DETAILS FOR JP2010519027\|Actual or expected expiration date=2018-08-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=JP Corresponding appl: JP2009550646\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2009JP-0550646\|Corresponding cc:\|Designated or member state=JP Corresponding pat: JP2010519027\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2010-06-03\|Publication number in the designated or member state=JP2010519027\|Event publication date=2009-08-20\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=JP\|Event publication date=2018-08-23\|Event code=JP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=JP\|MEMBER STATE LEGAL DETAILS FOR KR10-2009-0125109\|Actual or expected expiration date=2018-06-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=KR Corresponding appl: KR10-2009-7019662\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2009KR-7019662\|Corresponding cc:\|Designated or member state=KR Corresponding pat: KR10-2009-0125109\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2009-12-03\|Publication number in the designated or member state=KR20090125109\|Event publication date=2009-09-21\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=KR\|Event publication date=2018-06-04\|Event code=KR/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=KR\|MEMBER STATE LEGAL DETAILS FOR US20100021362\|Actual or expected expiration date=2021-09-06\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=US Corresponding appl: US12527608\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2008US-12527608\|Corresponding cc:\|Designated or member state=US Corresponding pat: US20100021362\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2010-01-28\|Publication number in the designated or member state=US20100021362\|Event publication date=2009-09-18\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=US\|Event publication date=2024-08-13\|Event code=US/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=US\|(JP5345954)\|LEGAL DETAILS FOR JP5345954\|Actual or expected expiration date=2018-08-23\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=JP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=JP JP2009550646\|Application date=2008-02-20\|Standardized application number=2009JP-0550646\|Event publication date=2010-06-03\|Event code=JP/A\|Event group=Examination events\|Published application\|Publication country=JP\|Publication number=JP2010519027\|Publication stage code=A\|Publication date=2010-06-03\|Standardized publication number=JP2010519027\|Event publication date=2011-02-08\|Event code=JP/A621\|Event indicator=Pos\|Event group=Examination events\|Written request for application examination\|Japanese intermediate code: A621\|Effective date of the event=2011-02-07\|Event publication date=2012-05-28\|Event code=JP/A977\|Event group=Examination events\|Report on retrieval\|Japanese intermediate code: A971007\|Effective date of the event=2012-05-28\|Event publication date=2012-06-06\|Event code=JP/A131\|Event indicator=Neg\|Event group=Examination events\|Notification of reasons for refusal\|Japanese intermediate code: A131\|Effective date of the event=2012-06-05\|Event publication date=2012-08-25\|Event code=JP/A521\|Event group=Restitution or restoration Corrections\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2012-08-24\|Event publication date=2013-04-03\|Event code=JP/A131\|Event indicator=Neg\|Event group=Examination events\|Notification of reasons for refusal\|Japanese intermediate code: A131\|Effective date of the event=2013-04-02\|Event publication date=2013-07-02\|Event code=JP/A521\|Event group=Restitution or restoration Corrections\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2013-07-01\|Event publication date=2013-07-19\|Event code=JP/TRDD\|Event indicator=Pos\|Event group=Administrative notifications\|Trial decision date\|Event publication date=2013-07-24\|Event code=JP/A01\|Event indicator=Pos\|Event group=Event indicating In Force\|Written decision to grant a patent or to grant a registration (utility model)\|Japanese intermediate code: A01\|Effective date of the event=2013-07-23\|Event publication date=2013-08-22\|Event code=JP/A61\|Event indicator=Pos\|Event group=Event indicating In Force\|First payment of annual fees (during grant procedure)\|Japanese intermediate code: A61\|Effective date of the event=2013-08-15\|Event publication date=2013-08-23\|Event code=JP/R150\|Event indicator=Pos\|Event group=Event indicating In Force\|CERTIFICATE OF PATENT OR REGISTRATION OF UTILITY MODEL\|Japanese intermediate code: R150\|Event publication date=2013-11-20\|Event code=JP/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Published granted patent (Second level) from 01-03-1996 onwards (Published examined patent application (Second level) 1971-1996)\|Publication country=JP\|Publication number=JP5345954\|Publication stage code=B2\|Publication date=2013-11-20\|Standardized publication number=JP5345954\|Event publication date=2016-08-02\|Event code=JP/R250\|Event indicator=Pos\|Event group=Payment or non-payment notifications Restitution or restoration\|Receipt of annual fees\|Japanese intermediate code: R250\|Event publication date=2017-08-22\|Event code=JP/R250\|Event indicator=Pos\|Event group=Payment or non-payment notifications Restitution or restoration\|Receipt of annual fees\|Japanese intermediate code: R250\|Event publication date=2018-08-23\|Event code=JP/LAPS\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Cancellation because of no payment of annual fees\|(CN101641145)\|LEGAL DETAILS FOR CN101641145\|Actual or expected expiration date=2018-02-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN200880006610\|Application date=2008-02-20\|Standardized application number=2008CN-80006610\|Event publication date=2010-02-03\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN101641145\|Publication stage code=A\|Publication date=2010-02-03\|Standardized publication number=CN101641145\|Event publication date=2010-02-03\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2010-03-24\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2014-05-07\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN101641145\|Publication stage code=B\|Publication date=2014-05-07\|Standardized publication number=CN101641145B\|Event publication date=2014-05-07\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2019-02-15\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee\|Effective date of the event=2018-02-20\|(IN293376)\|LEGAL DETAILS FOR IN293376\|Actual or expected expiration date=2028-02-20\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2009-09-18\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN6026/DELNP/2009\|Application date=2009-09-18\|Standardized application number=2009IN-DN06026\|Event publication date=2011-08-26\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN6026/DELNP/2009\|Publication stage code=A\|Publication date=2011-08-26\|Standardized publication number=IN2009DN06026\|Event publication date=2018-02-26\|Event code=IN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent\|Publication country=IN\|Publication number=IN293376\|Publication stage code=B\|Publication date=2018-02-26\|Standardized publication number=IN-293376\|(CA2678800)\|LEGAL DETAILS FOR CA2678800\|Actual or expected expiration date=2019-02-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2678800\|Application date=2008-02-20\|Standardized application number=2008CA-2678800\|Event publication date=2008-08-28\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2678800\|Publication stage code=A1\|Publication date=2008-08-28\|Standardized publication number=CA2678800\|Event publication date=2013-02-05\|Event code=CA/EEER\|Event indicator=Pos\|Event group=Examination events\|Examination request\|Effective date of the event=2013-01-23\|Event publication date=2015-11-24\|Event code=CA/C\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent (second level)\|Publication country=CA\|Publication number=CA2678800\|Publication stage code=C\|Publication date=2015-11-24\|Standardized publication number=CA2678800\|Event publication date=2019-04-03\|Event code=CA/MKLA\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Lapsed\|Effective date of the event=2019-02-20\|(KR10-1527365)\|LEGAL DETAILS FOR KR10-1527365\|Actual or expected expiration date=2018-06-04\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=KR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=KR KR10-2009-7019662\|Application date=2008-02-20\|Standardized application number=2009KR-7019662\|Event publication date=2009-12-03\|Event code=KR/A\|Event group=Examination events\|Published application\|Publication country=KR\|Publication number=KR10-2009-0125109\|Publication stage code=A\|Publication date=2009-12-03\|Standardized publication number=KR20090125109\|Event publication date=2013-01-21\|Event code=KR/A201\|Event group=Examination events\|Request for examination\|Event publication date=2014-03-28\|Event code=KR/E902\|Event indicator=Neg\|Event group=Examination events\|Notification of reason for refusal\|Event publication date=2014-09-26\|Event code=KR/E902\|Event indicator=Neg\|Event group=Examination events\|Notification of reason for refusal\|Event publication date=2015-03-16\|Event code=KR/E701\|Event indicator=Pos\|Event group=Examination events\|Decision to grant or registration\|Event publication date=2015-06-03\|Event code=KR/GRNT\|Event indicator=Pos\|Event group=Examination events\|Written decision to grant\|Event publication date=2015-06-22\|Event code=KR/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent specification\|Publication country=KR\|Publication number=KR10-1527365\|Publication stage code=B1\|Publication date=2015-06-22\|Standardized publication number=KR101527365\|Event publication date=2018-06-04\|Event code=KR/LAPS\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Lapse due to unpaid annual fee\|(AU2008217572)\|LEGAL DETAILS FOR AU2008217572\|Actual or expected expiration date=2018-09-13\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=2008-02-20\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2008217572\|Application date=2008-02-20\|Standardized application number=2008AU-0217572\|Event publication date=2008-08-28\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2008217572\|Publication stage code=A1\|Publication date=2008-08-28\|Standardized publication number=AU2008217572\|Event publication date=2010-02-04\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent proceeded by OPI\|Publication country=AU\|Publication number=AU2008217572\|Publication stage code=B2\|Publication date=2010-02-04\|Standardized publication number=AU2008217572\|Event publication date=2010-06-03\|Event code=AU/FGA\|Event indicator=Pos\|Event group=Event indicating In Force\|Letters patent sealed or granted (standard patent)\|Event publication date=2018-09-13\|Event code=AU/MK14\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent ceased section 143(a) (annual fees not paid) or expired\|(AU2009250983)\|LEGAL DETAILS FOR AU2009250983\|Actual or expected expiration date=2010-12-02\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2009-12-16\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2009250983\|Application date=2009-12-16\|Standardized application number=2009AU-0250983\|Event publication date=2010-01-14\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2009250983\|Publication stage code=A1\|Publication date=2010-01-14\|Standardized publication number=AU2009250983\|Event publication date=2010-12-02\|Event code=AU/MK1\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application lapsed section 142(2)(a) - no request for examination in relevant period	(EP2134449)\|Contracting States: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, GB, IE, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2008/101293)\|ARIPO: GH, GM, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2008/101293)\|EAPO: RU, TJ, BY, MD, AZ, TM, AM, KG, KZ\|(WO2008/101293)\|EPO: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, GB, IE, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2008/101293)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2008/101293)\|National States: PT, HN, HR, HU, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, KM, KN, SV, CH, KP, SY, KR, CN, CO, CR, KZ, CU, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PG, PH, PL	(WO2008/101293)\|IN\|(IN293376)\|IN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=EVho024Sjd+0uo6WVhVzAWkyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP0000000004241227&ekey=2389&xpn=EP2134449&kind=B1	https://register.epo.org/application?number=EP08706115	https://permalink.orbit.com/RenderStaticFirstPage?XPN=ZwTaFI0pS2A1zTc2PWcWRHfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	AU	(WO2008/101293)\|AU	(WO2008/101293)\|NAME=HUNWICK, Richard J. Level 13, 221 Miller Street, North Sydney, New South Wales 2060 , COUNTRY=AU	(EP2134449)\|GB\|(EP2134449)\|GB\|(EP2134449)\|GB\|\|(US20100021362)\|US\|(WO2008/101293)\|AU\|\|\|\|\|(CA2678800)\|CA\|(CA2678800)\|CA\|	(EP2134449)\|NAME=Williams, Richard Andrew Norman;Harrison Goddard Foote 8th Floor 140 London Wall , CITY=London EC2Y 5DN , COUNTRY=GB , REG=100754772\|(EP2134449)\|NAME=Williams, Richard Andrew Norman Harrison Goddard Foote , CITY=40- 43 Chancery LaneLondon WC2A 1JA , COUNTRY=GB , REG=100754772\|(EP2134449)\|NAME=Williams, Richard Andrew Norman;Harrison Goddard Foote 40- 43 Chancery Lane , CITY=LondonWC2A 1JA , COUNTRY=GB , REG=09210841\|(US8496897)\|NAME=Frommer Lawrence & Haug LLP NAME=Santucci Ronald R\|(US20100021362)\|NAME=FROMMER LAWRENCE & HAUG 745 FIFTH AVENUE- 10TH FL. , CITY=NEW YORK , STATE=NY , POSTCODE=10151 , COUNTRY=US\|(WO2008/101293)\|NAME=GRIFFITH HACK Level 29, Northpoint, 100 Miller Street, North Sydney, New South Wales 2060 , COUNTRY=AU\|(JP5345954)\|NAME=YOSHIDA Kenji , REG=100075258NAME=ISHIDA Jun , REG=100096976\|(JP2010519027)\|NAME=YOSHIDA Kenji , REG=100075258NAME=ISHIDA Jun , REG=100096976\|(CN101641145)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(CN101641145)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(CA2678800)\|NAME=MBM INTELLECTUAL PROPERTY LAW LLP , COUNTRY=CA\|(CA2678800)\|NAME=MBM INTELLECTUAL PROPERTY LAW LLP , COUNTRY=CA\|(KR10-2009-0125109)\|NAME=HALLA PATENT & LAW FIRM	(EP2134449)\|AU\|(EP2134449)\|AU\|(EP2134449)\|AU\|(US8496897)\|AU\|(US20100021362)\|AU\|(WO2008/101293)\|AU\|\|\|\|\|\|(IN6026/DELNP/2009)\|AU\|(CA2678800)\|AU\|(CA2678800)\|AU\|\|\|\|\|	(EP2134449)\|NAME=Hunwick, Richard J. 59 Abingdon Road, CITY=Roseville NSW 2069, COUNTRY=AU\|(EP2134449)\|NAME=Hunwick, Richard J. 59 Abingdon Road, CITY=Roseville NSW 2069, COUNTRY=AU\|(EP2134449)\|NAME=Hunwick, Richard J. 221 Miller Street Level 13, CITY=North Sydney, NSW 2060, COUNTRY=AU\|(US8496897)\|NAME=Hunwick Richard J, CITY=North Sydney, COUNTRY=AU\|(US20100021362)\|NAME=Hunwick Richard J., CITY=New South Wales, COUNTRY=AU\|(WO2008/101293)\|NAME=HUNWICK, Richard J. Level 13, 221 Miller Street, North Sydney, New South Wales 2060, COUNTRY=AU\|(JP5345954)\|NAME=Richard Jay Han Wick\|(JP2010519027)\|NAME=Richard Jay Han Wick\|(CN101641145)\|NAME=HUNWICK RICHARD J.\|(CN101641145)\|NAME=HUNWICK RICHARD J.\|(IN293376)\|NAME=HUNWICK RICHARD J\|(IN6026/DELNP/2009)\|NAME=HUNWICK RICHARD J, COUNTRY=AU\|(CA2678800)\|NAME=HUNWICK, RICHARD J., COUNTRY=AU\|(CA2678800)\|NAME=HUNWICK, RICHARD J., COUNTRY=AU\|(KR10-1527365)\|NAME=HUNWICK RICHARD J.\|(KR10-2009-0125109)\|NAME=HUNWICK RICHARD J.\|(AU2008217572)\|NAME=RICHARD J. HUNWICK\|(AU2008217572)\|NAME=RICHARD J. HUNWICK\|(AU2009250983)\|NAME=RICHARD HUNWICK	(WO2008/101293)\|5\|(AU2009250983)\|5\|(IN293376)\|5\|(CA2678800)\|5\|(KR10-1527365)\|5\|(CN101641145)\|5\|(JP5345954)\|5\|(US8496897)\|5\|(EP2134449)\|5\|(AU2008217572)\|5	6	10			(EP2134449)\|WO2008/101293\|(US8496897)\|WO2008/101293\|(JP5345954)\|WO2008/101293\|(CN101641145)\|WO2008/101293\|(IN293376)\|WO2008/101293\|(CA2678800)\|WO2008/101293\|(KR10-1527365)\|WO2008/101293\|(AU2008217572)\|WO2008/101293\|(AU2009250983)\|WO2008/101293		(EP2134449)\|Number of Claims: NCL=21\|Primary examiner: Burkhardt, Thorsten\|\|Primary examiner: Burkhardt, Thorsten\|\|Primary examiner: Burkhardt, Thorsten\|\|(US8496897)\|Number of Claims: NCL=20\|Number of Drawings: NDR=7\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1,18\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=412\|Primary examiner: Silverman Stanley\|Art Unit.: ART =1736\|\|(US20100021362)\|Number of Claims: NCL=32\|Number of Drawings: NDR=8\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1,21,27,28,33\|Number of Independent Claims: NICL=5\|Exemplary Claim Number: ECL=1\|Primary examiner: Silverman Stanley\|Art Unit.: ART =1736\|\|(WO2008/101293)\|Number of Claims: NCL=46\|Extended kind: EXTK=x\|\|(JP5345954)\|Number of Claims: NCL=35\|Number of Pages: NPAGES=22\|Request for examination: REQEXA=false\|\|(JP2010519027)\|Number of Claims: NCL=46\|Number of Pages: NPAGES=28\|Request for examination: REQEXA=false\|\|(CN101641145)\|Number of Claims: NCL=28\|Gazette date: GAZDATE=2014-05-07\|Gazette number: GAZNUM=30-19\|Substantial examination effective date: 20100324 Examination duration: 49 months\|Number of Pages: NPAGES=24\|Primary examiner: Wang Yigang\|Primary examiner: 王义刚\|\|(CN101641145)\|Number of Claims: NCL=46\|Gazette date: GAZDATE=2010-02-03\|Gazette number: GAZNUM=26-05\|Substantial examination effective date: 20100324 Examination duration: 49 months\|Number of Pages: NPAGES=35\|Primary examiner: Wang Yigang\|Primary examiner: 王义刚\|\|(IN293376)\|Number of Claims: NCL=21\|\|(CA2678800)\|Number of Claims: NCL=43\|Number of Pages: NPAGES=44\|\|(CA2678800)\|Number of Claims: NCL=43\|Number of Pages: NPAGES=44\|\|(KR10-1527365)\|Number of Claims: NCL=28\|\|(KR10-2009-0125109)\|Number of Claims: NCL=32\|Number of Pages: NPAGES=26\|\|(AU2008217572)\|Number of Claims: NCL=32\|\|(AU2009250983)\|Number of Claims: NCL=46\|	(US8496897)\|Previous publication: US20100021362 A1 2010-01-28 [US20100021362]\|(AU2009250983)\|Division of: AU2008217572 FDD=2008-02-20 [2008AU-0217572]	(EP2134449)\|ENGLISH (ENG)	(IN-293376)\|Patent\|(CA2678800)\|Patent\|(KR101527365)\|Patent\|(CN101641145B)\|Patent\|(JP5345954)\|Patent\|(US8496897)\|Patent\|(EP2134449)\|Patent\|(IN2009DN06026)\|Patent\|(EP2134449)\|Patent\|(JP2010519027)\|Patent\|(AU2008217572)\|Patent\|(CN101641145)\|Patent\|(US20100021362)\|Patent\|(AU2009250983)\|Patent\|(EP2134449)\|Patent\|(KR20090125109)\|Patent\|(AU2008217572)\|Patent\|(CA2678800)\|Patent\|(WO2008101293)\|Patent	Titre: (EP2134449)\|System, apparatus and method for carbon dioxide sequestration Résumé: (EP2134449)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.	6	Abstract	gpt-4o-mini	yes	The process described involves the use of metal silicate rocks to capture CO₂ and convert it into metal carbonates, which aligns with the topic of enhanced weathering and carbon sequestration.
8	CN202410172022	CN202410172022	CN118134720	110028832	CN118134720 A 2024-06-04 [CN118134720]	2024-02-06	2024-02-06	2024-06-04		(CN118134720)\|2044-02-06	(CN118134720)\|Farmland carbon sequestration and sink increase method, system and equipment based on silicate rock weathering	(CN118134720)\|The invention provides a farmland carbon sequestration and sink increase method, system and equipment based on silicate rock weathering, and the method comprises the steps: obtaining agricultural management basic data; wherein the agricultural management basic data comprises silicate weathering carbon sink data, farmland environment data, soil carbon flux carbon emission data and agricultural management carbon emission data; calculating agricultural production management carbon emission according to the agricultural management basic data; acquiring a preset farmland carbon emission target value; and adjusting farmland management measures according to a preset farmland carbon emission target value and the agricultural production management carbon emission. According to the method, the agricultural production management carbon emission can be calculated, the problem that the farmland carbon emission is unknown after the silicate rock-based carbon sequestration and fertility improvement agent is added is solved, the agricultural production management carbon emission can be accurately estimated, and data support is provided for achieving the carbon emission target. Farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and the preset farmland carbon emission target value.	CHONGQING HUADI ZIHUAN TECHNOLOGY\|CHONGQING INSTITUTE OF GEOLOGY & MINERAL RESOURCES	(CN118134720)\|CHONGQING INSTITUTE OF GEOLOGY AND MINERAL RESOURCES ([CN])\|CHONGQING HUADI ZIHUAN TECHNOLOGY CO., LTD.	MA LEI\|SI HONGTAO\|MAO ZHENG\|WANG CHEN\|LI CHENG\|XU MINGZE\|ZHU DONGXUE\|ZHU DAN\|XU WENXING	(CN118134720)\|MA LEI\|SI HONGTAO\|MAO ZHENG\|WANG CHEN\|LI CHENG\|XU MINGZE\|ZHU DONGXUE\|ZHU DAN\|XU WENXING	(CN118134720)\|YU HONG;CHONGQING ZHI HUI ZHI YUAN INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP)\|Reg. Nb: 50234	(CN118134720)\|Compared with the prior art, the invention has the advantages that: the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation fertilizer-increasing modifier, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for carbon peak and carbon neutralization in the farmland field.\|Those of ordinary skill in the art will appreciate that: the discussion of any of the embodiments above is merely exemplary and is not intended to suggest that the scope of the invention (including the claims) is limited to these examples; the technical features of the above embodiments or in the different embodiments may also be combined within the idea of the invention, the steps may be implemented in any order, and there are many other variations of the different aspects of the embodiments of the invention as described above, which are not provided in detail for the sake of brevity.\|	(CN118134720)\|1. A farmland carbon fixation and sink enhancement method based on silicate rock weathering is characterized by comprising the following steps: Acquiring basic agricultural management data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; calculating an agricultural production management carbon emission amount according to the agricultural management basic data; acquiring a preset farmland carbon emission target value; And adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission.\|	(CN118134720)\|The invention provides a method, a system and equipment for carbon fixation and sink enhancement of farmland based on silicate rock weathering, wherein the method comprises the following steps: acquiring basic agricultural management data; wherein, the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; calculating an agricultural production management carbon emission amount according to the agricultural management basic data; acquiring a preset farmland carbon emission target value; and adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission.\|The invention relates to a farmland carbon fixation and exchange increase method, system and equipment based on silicate rock weathering.\|Therefore, the invention provides a farmland carbon fixation and collection increasing method based on silicate rock weathering, which comprises the steps of firstly obtaining agriculture management basic data, then calculating the agriculture production management carbon emission according to the agriculture management basic data, and then judging whether to adjust farmland management measures according to the agriculture production management carbon emission and a preset farmland carbon emission target value.\|	(CN118134720)\|SILICATE(100,71)\|PRESET FARMLAND CARBON EMISSION(100,28)\|CARBON FIXATION(100,19)\|FARMLAND(100,17)\|FARMLAND CARBON FIXATION(100,7)\|EQUIPMENT(100,4)\|FARMLAND MANAGEMENT(93,7)\|FARMLAND CARBON EMISSION(86,41)\|AGRICULTURAL PRODUCTION MANAGEMENT(84,47)\|AGRICULTURAL MANAGEMENT(69,57)\|CARBON EMISSION(55,135)\|CARBON SEQUESTRATION(55,66)\|FARMLAND ENVIRONMENT DATA(49,16)\|SOIL CARBON FLUX(45,25)\|ADJUSTING FARMLAND MANAGEMENT(45,8)\|PRESET SILICATE WEATHERING(45,3)\|AGRICULTURE PRODUCTION MANAGEMENT(45,2)\|CROP PLANTING(43,13)\|UNCLEAR FARMLAND(43,3)\|UNCLEAR FARMLAND CARBON FIXATION(43,3)\|TARGET VALUE(39,26)\|OBTAINING AGRICULTURE MANAGEMENT(39,1)\|FARMLAND CARBON SEQUESTRATION(37,5)\|CROP ECONOMIC COEFFICIENT(37,4)\|AGRICULTURAL MANAGEMENT DATA(37,3)\|MANAGEMENT REVISION MODULE(36,3)\|UNKNOWN FARMLAND CARBON EMISSION(36,1)\|CARBON SEQUESTRATION DATA(35,24)\|FARMLAND MANAGEMENT MEASURE(35,4)\|CARBON EMISSION DATA(34,41)\|PRESET CROP(34,8)\|BASIC AGRICULTURAL MANAGEMENT DATA(34,3)\|SOIL CARBON EMISSION(33,16)\|TRAINING(32,16)\|FERTILIZER INCREASING MODIFIER(32,1)\|CARBON SEQUESTRATION MODEL(31,14)\|AGRICULTURAL MANAGEMENT BASIC DATA(31,4)\|EMISSION CALCULATION MODULE(30,2)\|CROP SOIL TEXTURE(29,3)\|AGRICULTURAL MANAGEMENT ACQUISITION(29,2)\|SILICATE WEATHERED CARBON SEQUESTRATION(29,1)\|INPUTTING SILICATE(27,3)\|ROCK CARBON FIXATION(27,2)\|DATA BASIS(26,9)\|CARBON NEUTRALIZATION(26,3)\|AGRICULTURE MANAGEMENT(26,1)\|AGRICULTURAL MANAGEMENT BASE DATA(25,14)\|AGRICULTURAL MANAGEMENT CARBON EMISSION(25,12)\|AGRICULTURE MANAGEMENT BASIC DATA(24,1)\|TECHNICAL FEATURE(24,1)\|IRRIGATION CARBON EMISSION COEFFICIENT(23,3)\|OBTAINING CARBON PLANTING(23,3)\|PESTICIDE CARBON EMISSION COEFFICIENT(23,3)\|PRESET AGRICULTURAL MANAGEMENT(23,3)\|UNCLEAR CARBON EMISSION(23,3)\|CARBON SINK MODEL(22,14)\|AGRICULTURAL PRODUCTION MANAGEMENT CALCULATION(22,2)\|BREVITY(22,1)\|EXOGENOUS SILICATE ROCK ADDITION(21,9)\|O TH CULTIVATION(21,6)\|PRESET TARGET(21,2)\|CROP FARMLAND AREA(20,3)\|SILICATE PREDICTION MODEL(20,3)\|PRODUCTION MANAGEMENT(20,2)\|NETWORK SOURCE(19,12)\|CROP GROWTH CARBON SINK(19,3)\|TARGET ACQUISITION MODULE(19,2)\|CALCULATED AGRICULTURAL PRODUCTION MANAGEMENT(18,3)\|CARBON PEAK(18,3)\|CARBON EMISSION TARGET(18,1)\|MOISTURE CONTENT(17,4)\|CARBON SINK DATA(15,17)\|RAINFALL(14,4)\|N TH PESTICIDE(14,3)\|PRESET CARBON EMISSION(14,3)\|INPUTTING CARBON EMISSION DATA(14,1)\|UNUTILIZED MINE TAILING(14,1)\|GROUND(13,5)\|RANDOM FOREST(13,5)\|CROP CARBON FLUX DATA(13,3)\|GROWTH PERIOD(13,3)\|SUPPORTING DATA(12,4)\|CARBON EMISSION MODEL(12,3)\|SILICATE ROCK PARTICLE SIZE(11,4)\|FERTILIZER ENHANCEMENT MODIFIER(11,1)\|SILICATE ROCK WEATHERING(11,1)\|AGRICULTURAL MACHINE CARBON EMISSION(10,5)\|CHEMICAL FERTILIZER CARBON EMISSION(10,4)\|NEURAL NETWORK(10,4)\|ROOT CAP RATIO(10,4)\|SINK INCREASING DATA(10,4)\|DATA ACQUISITION MODULE(10,3)\|FARMLAND FIELD(9,3)\|NONLINEAR FUNCTION MODEL(9,3)\|COMPREHENSIVE GREEN TRANSFORMATION(8,1)\|ORGANIC SUBSTANCE(7,3)\|FARMLAND CULTIVATION CARBON EMISSION(7,1)\|REALIZING FARMLAND(7,1)\|SYNERGY PROMOTION(7,1)\|COMMUNICATION INTERFACE(6,4)\|ACCELERATE SILICATE(6,1)\|AM VM M(6,1)\|FARMLAND SOIL(6,1)\|POTASSIUM FELDSPAR(6,1)\|SOIL ECOSYSTEM(6,1)\|VEGETATION RECOVERY(6,1)\|AGRICULTURAL MANAGEMENT MEASURE DATA(5,3)\|COMMUNICATION MODULE(5,2)\|CROP PLANTED CARBON SEQUESTRATION(5,1)\|DISTRIBUTED SCENARIO(5,1)\|DISTRIBUTED SCENE(5,1)\|ECOLOGICAL ENVIRONMENT(5,1)\|ECONOMY DEVELOPMENT(5,1)\|ENERGY UTILIZATION IMPORTANCE(5,1)\|QUICK CALCULATION(5,1)\|AGRICULTURAL MACHINE FUEL INFORMATION(4,2)\|PRECIPITATION(4,2)\|AL UL L(4,1)\|AUTOMATIC CALCULATION(4,1)\|COMMUNICATION INTERACTION(4,1)\|CROP GROWTH CONDITION(4,1)\|CULTIVATION MODE(4,1)\|ECOLOGICAL CIVILIZATION CONSTRUCTION(4,1)\|ENHANCED SILICATE(4,1)\|EQUIVALENT SUBSTITUTION(4,1)\|ESTIMATED AGRICULTURAL PRODUCTION MANAGEMENT(4,1)\|IDENTIFICATION MODEL(4,1)\|NEGATIVE EMISSION(4,1)\|OBTAINING AGRICULTURAL MANAGEMENT(4,1)\|ORDINARY MEANING(4,1)\|POSITIONAL RELATIONSHIP(4,1)\|PRESET SOIL CARBON FLUX(4,1)\|	(CN118134720)\|1. A farmland carbon fixation and sink enhancement method based on silicate rock weathering is characterized by comprising the following steps:\| Acquiring basic agricultural management data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \| calculating an agricultural production management carbon emission amount according to the agricultural management basic data; \| acquiring a preset farmland carbon emission target value; \| And adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|2. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering of claim 1, wherein the calculating the agricultural production management carbon emissions from the agricultural management base data comprises:\| Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \| Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \| obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \| obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \| And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|3. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 2, wherein the training process of the silicate-weathered carbon sequestration model comprises:\| Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \| the carbon sink model for the weathering of the preset silicate comprises the following components: \|Wx=F(x,y,q,d)\| Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|4. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 2, wherein the training process of the carbon sequestration model for crop planting comprises:\| Obtaining carbon planting and sink increasing data according to the farmland environment data; \| The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \| wherein, the carbon sequestration model for the preset crop planting comprises: \|Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\| Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|5. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 2, wherein the training process of the carbon emission model of the soil carbon flux comprises:\| Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \| Wherein, the carbon emission model of the preset soil carbon flux comprises: \|Fp=∑Ti·Ai,ki·ti\| Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|6. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering of claim 2, wherein the training process of the carbon emission model for agricultural management comprises:\| The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \| wherein, the carbon emission model of preset agricultural management includes: \|Mp=M1+M2+M3+M4\|M1=∑Al·Ul·αl\|M2=∑Am·Vm·αm\|M3=∑An·Wn·αn\|M4=∑Ao·αo\| Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|7. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 2, wherein the silicate rock weathering farmland carbon emission prediction model comprises:\|S=Mp+Fp-Wx-Zx\| Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|8. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 1, wherein the adjusting farmland management measures according to the preset target value of farmland carbon emission and the agricultural production management carbon emission comprises:\| judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \| and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|9. A silicate-based weathered farmland carbon sequestration and sequestration system for implementing a silicate-based weathered farmland carbon sequestration and sequestration method according to claims 1-8, comprising:\| the data acquisition module is used for acquiring the agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \| An emission calculation module for calculating an agricultural production management carbon emission amount according to the agricultural management base data; \| the target acquisition module is used for acquiring a preset farmland carbon emission target value; \| And the management revision module is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|10. An apparatus comprising a memory, a processor and a computer program stored on the memory and executable on the processor, wherein the processor implements the steps of the method of any one of claims 1 to 8 when the computer program is executed.	(CN118134720)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to a farmland carbon fixation and exchange increase method, system and equipment based on silicate rock weathering.\|BACKGROUND ART\|[0002] With the development of economy, the importance of effective energy utilization, environmental pollution reduction and climate change is increasingly highlighted. The ecological civilization construction of China enters a key period for promoting the synergy of pollution reduction and carbon reduction, promoting the comprehensive green transformation of economic and social development and realizing the change of the quality improvement of ecological environment from variable quantity to variable quality.\|[0003] Enhanced silicate rock weathering is a negative emission technique based on the geochemical principle that aims to accelerate the silicate rock chemical weathering process by adding silicate rock powder to farms or forests to fix more atmospheric CO 2 in a shorter time. The potassium feldspar mineral resources in China are rich, the reserves are huge, the grade is excellent, and a large amount of unutilized mine tailings and alkali silicate waste materials exist, so that the potential of removing the atmospheric CO 2 by enhancing the weathering of silicate rock is huge. At present, a calculation method for carbon emission of soil after silicate rock addition is not available, and a method for carbon fixation and sink increase of soil based on silicate rock weathering is not available.\|DISCLOSURE\|Disclosure of Invention\|[0004] Based on the above, it is necessary to provide a method, a system and a device for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering.\|[0005] A farmland carbon fixation and exchange increase method based on silicate rock weathering comprises the following steps:\|[0006] Acquiring basic agricultural management data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0007] calculating an agricultural production management carbon emission amount according to the agricultural management basic data; \|[0008] acquiring a preset farmland carbon emission target value; \|[0009] And adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|[0010] In one embodiment, calculating the agricultural production management carbon emissions from the agricultural management basis data includes:\|[0011] Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \|[0012] Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \|[0013] obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \|[0014] obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \|[0015] And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|[0016] In one embodiment, the training process for a silicate weathered carbon sink model includes:\|[0017] Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \|[0018] the carbon sink model for the weathering of the preset silicate comprises the following components: \|[0019] Wx=F(x,y,q,d)\|[0020] Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|[0021] In one of the embodiments of the present invention,\|[0022] The training process of the carbon sequestration model for crop planting comprises the following steps:\|[0023] Obtaining carbon planting and sink increasing data according to the farmland environment data; \|[0024] The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \|[0025] wherein, the carbon sequestration model for the preset crop planting comprises: \|[0026] Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\|[0027] Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|[0028] In one embodiment, the training process of the carbon emission model of the soil carbon flux comprises:\|[0029] Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \|[0030] Wherein, the carbon emission model of the preset soil carbon flux comprises: \|[0031] Fp=∑Ti·Ai,ki·ti\|[0032] Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|[0033] In one embodiment, the training process for an agricultural managed carbon emission model includes:\|[0034] The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \|[0035] wherein, the carbon emission model of preset agricultural management includes: \|[0036] Mp=M1+M2+M3+M4\|[0037] M1=∑Al·Ul·αl\|[0038] M2=∑Am·Vm·αm\|[0039] M3=∑An·Wn·αn\|[0040] M4=∑Ao·αo\|[0041] Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|[0042] In one embodiment, a silicate-weathered farmland carbon emission prediction model includes:\|[0043] S=Mp+Fp-Wx-Zx\|[0044] Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|[0045] In one embodiment, adjusting the farmland management measure according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount includes:\|[0046] judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \|[0047] and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|[0048] A farmland carbon sequestration and sequestration system based on silicate rock weathering is used for realizing the farmland carbon sequestration and sequestration method based on silicate rock weathering, and comprises the following steps:\|[0049] the data acquisition module is used for acquiring the agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0050] An emission calculation module for calculating an agricultural production management carbon emission amount according to the agricultural management base data; \|[0051] the target acquisition module is used for acquiring a preset farmland carbon emission target value; \|[0052] And the management revision module is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|[0053] An apparatus comprising a memory, a processor and a computer program stored on the memory and executable on the processor, the processor implementing the steps of a silicate rock weathering based farmland carbon sequestration and sequestration method as described in the various embodiments above when the program is executed.\|[0054] Compared with the prior art, the invention has the advantages that: the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation fertilizer-increasing modifier, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for carbon peak and carbon neutralization in the farmland field. Meanwhile, farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and a preset farmland carbon emission target value, and the aim of low carbon emission of agricultural production is achieved.\|DRAWINGS DESCRIPTION\|[0055] FIG. 1 is a schematic flow diagram of a method for carbon sequestration and sequestration in a farmland based on silicate rock weathering in an embodiment;\|[0056] FIG. 2 is a schematic diagram of a system for carbon sequestration and sequestration in a farmland based on silicate rock weathering in accordance with an embodiment; \|[0057] Fig. 3 is a schematic diagram of the internal structure of the apparatus in one embodiment. \|INVENTION MODE\|Detailed Description\|[0058] Before proceeding with the description of the embodiments of the present invention, the general inventive concept will be described as follows:\|[0059] The invention is mainly developed in the silicate rock farmland improvement process, and at present, a calculation method for carbon emission of soil after silicate rock addition is not available, and a method for carbon fixation and sink enhancement of soil based on silicate rock weathering is not available. \|[0060] Therefore, the invention provides a farmland carbon fixation and collection increasing method based on silicate rock weathering, which comprises the steps of firstly obtaining agriculture management basic data, then calculating the agriculture production management carbon emission according to the agriculture management basic data, and then judging whether to adjust farmland management measures according to the agriculture production management carbon emission and a preset farmland carbon emission target value. The invention realizes quick calculation of farmland carbon emission of different types of farmland soil, silicate rock types, silicate rock addition amount, silicate rock particle size and different cultivation modes, and provides decision support for farmland management.\|[0061] Having described the general inventive concept, the present invention will be further described in detail with reference to the accompanying drawings by way of specific embodiments thereof, in order to make the objects, technical solutions and advantages of the present invention more apparent.\|[0062] It should be noted that unless otherwise defined, technical or scientific terms used in one or more embodiments of the present specification should be given the ordinary meaning as understood by one of ordinary skill in the art to which the present invention pertains. The use of the terms "first," "second," and the like in one or more implementations of the present description does not denote any order, quantity, or importance, but rather the terms "first," "second," and the like are used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that elements or items preceding the word are included in the element or item listed after the word and equivalents thereof, but does not exclude other elements or items. The terms "connected" or "connected," and the like, are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", etc. are used merely to indicate relative positional relationships, which may also be changed when the absolute position of the object to be described is changed.\|[0063] For convenience of understanding, the terms involved in the embodiments of the present invention are explained below:\|[0064] Carbon sink is the process, activity or mechanism of absorbing carbon dioxide in the atmosphere by means of tree planting, vegetation recovery and the like, thereby reducing the concentration of greenhouse gases in the atmosphere. Land ecosystems such as forests, grasslands, wetlands, farmlands, deserts, cities and the like and marine ecosystems are important carbon sinks. \|[0065] Carbon sequestration and sequestration means that the carbon dioxide absorption and storage capacity of an ecosystem are increased by various means and measures, thereby reducing the concentration of carbon dioxide in the atmosphere.\|[0066] In one embodiment, as shown in fig. 1, there is provided a method for carbon sequestration and sequestration in a farmland based on silicate rock weathering, comprising the steps of:\|[0067] Step S101, obtaining agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux, and carbon emission data for agricultural management. \|[0068] Specifically, agricultural management base data is acquired, the agricultural management base data including: carbon sink data based on silicate weathering, farmland environment data based on crop planting, carbon emission data based on soil carbon flux, and carbon emission data based on agricultural management. Wherein the carbon sink data based on silicate weathering comprises: silicate rock type, particle size, precipitation, application amount, weathered carbon sequestration data and the like; the farmland environment data based on crop planting includes: crop growth conditions, climate, weather, air quality, temperature and humidity and the like; carbon emission data based on soil carbon flux includes: carbon flux data, field area data, crop planting time and the like of different crop planting based on exogenous silicate rock addition; carbon emission data based on agricultural management includes: agricultural machine usage data, various kinds of agricultural machine fuel information, agricultural management measure data, and the like.\|[0069] Step S102, calculating the agricultural production management carbon emission amount according to the agricultural management basic data.\|[0070] Specifically, the estimated agricultural production management carbon emission amount can be calculated from the agricultural management base data.\|[0071] On this basis, calculating the agricultural production management carbon emission amount from the agricultural management basis data includes:\|[0072] Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \|[0073] Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \|[0074] obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \|[0075] obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \|[0076] And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|[0077] Specifically, a silicate-weathered carbon sink model based on silicate-weathered silicate is built, a crop-planted carbon sequestration model based on crop planting, a soil carbon flux carbon emission model based on soil respiration and an agricultural management carbon emission model based on agricultural production management are built, a silicate-weathered farmland carbon emission prediction model is built, and the agricultural production management carbon emission amount is obtained through the silicate-weathered farmland carbon emission prediction model.\|[0078] In the embodiment, the carbon emission amount of agricultural production management is calculated by establishing a plurality of models, so that the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation and fertilizer enhancement modifier are solved, the carbon emission amount of agricultural production management can be estimated accurately, and data support is provided for ' carbon peak and ' carbon neutralization ' in the farmland field.\|[0079] On the basis, the training process of the silicate weathered carbon sink model comprises the following steps:\|[0080] Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \|[0081] the carbon sink model for the weathering of the preset silicate comprises the following components: \|[0082] Wx=F(x,y,q,d)\|[0083] Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|[0084] Specifically, a carbon sink model of pre-set silicate weathering based on a random forest algorithm is constructed, W x =f (x, y, q, d). Wherein, F () represents a nonlinear function model of silicate-decomposed carbon sequestration and silicate type, rainfall, silicate application, silicate grain size constructed by random forest algorithm. And training a carbon sink model of the preset silicate weathering through the training data set to obtain the carbon sink model of the silicate weathering which meets the expectations. And acquiring silicate rock type, particle size, precipitation, application amount and weathered carbon fixation data, and calculating the carbon dioxide fixation amount generated by silicate rock weathering, namely the carbon sink amount generated by exogenous silicate rock addition.\|[0085] On the basis, the training process of the carbon sequestration model for crop planting comprises the following steps:\|[0086] Obtaining carbon planting and sink increasing data according to the farmland environment data; \|[0087] The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \|[0088] wherein, the carbon sequestration model for the preset crop planting comprises: \|[0089] Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\|[0090] Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|[0091] Specifically, farmland environment data are obtained, and carbon planting and collection increasing data of a target area are obtained through the existing identification model. Wherein, the carbon planting and sink increasing data comprises: crop type information and plant type information, crop weight information, moisture content of harvested part of crops, root cap ratio of crops and economic coefficient of crops.\|[0092] And constructing a carbon sequestration model Z x=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi for the preset crop planting based on the crop planting, training the carbon sequestration model for the preset crop planting through a training data set to obtain a carbon sequestration model which accords with the expected crop planting, and calculating the carbon sequestration amount generated by the crop growth according to the carbon sequestration data.\|[0093] On the basis, the training process of the carbon emission model of the soil carbon flux comprises the following steps:\|[0094] Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \|[0095] Wherein, the carbon emission model of the preset soil carbon flux comprises: \|[0096] Fp=∑Ti·Ai,ki·ti\|[0097] Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|[0098] Specifically, a multiple regression relation between measured carbon flux data and crop planting types and soil textures is constructed, a carbon emission model of the preset soil carbon flux based on the crop types and the soil textures is determined, F p=∑Ti·Ai,ki·ti, and training of the carbon emission model of the preset soil carbon flux is carried out through a training data set, so that a carbon emission model which accords with expected soil carbon flux is obtained. And obtaining carbon flux data, field area data and crop planting time based on different crop planting of exogenous silicate rock addition, and calculating to obtain the carbon emission of the soil.\|[0099] In the embodiment, based on the BP neural network, a multiple regression relation between actually measured exogenous silicate rock added carbon flux data and crop planting types and soil textures is constructed, and the automatic calculation of the carbon emission of the soil can be realized by operating the constructed carbon emission model of the soil carbon flux.\|[0100] On this basis, the training process of the carbon emission model of agricultural management comprises the following steps:\|[0101] The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \|[0102] wherein, the carbon emission model of preset agricultural management includes: \|[0103] Mp=M1+M2+M3+M4\|[0104] M1=∑Al·Ul·αl\|[0105] M2=∑Am·Vm·αm\|[0106] M3=∑An·Wn·αn\|[0107] M4=∑Ao·αo\|[0108] Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|[0109] Specifically, the use data of the agricultural machine is obtained, the agricultural management carbon emission is calculated by combining the agricultural management measure data, and the agricultural production carbon emission information is obtained. Various agricultural machine usage data include: fuel oil information of various kinds of agricultural machines, time length information of various kinds of agricultural machines, power information of various kinds of agricultural machines, and use quantity information of various kinds of agricultural machines; acquiring carbon emission factor information of various fuels based on the fuel information of various agricultural machines, and multiplying the carbon emission factor information of various fuels, the power information of various agricultural machines, the time-length information of various agricultural machines and the use quantity information of various agricultural machines to obtain the carbon emission quantity of the agricultural machines; obtaining chemical fertilizer use information and pesticide use information according to the agricultural management measure data, obtaining chemical fertilizer carbon emission factor information of various types and pesticide carbon emission factor information of various types based on the chemical fertilizer use information and the pesticide use information, calculating the product of the chemical fertilizer use information and the carbon emission factor of the corresponding chemical fertilizer type as chemical fertilizer carbon emission amount, and calculating the product of the pesticide use information and the carbon emission factor of the corresponding pesticide type as pesticide carbon emission amount; calculating the product of the cultivation and irrigation use information and the carbon emission factors of the corresponding modes as the carbon emission amount of farmland cultivation and irrigation; and combining the carbon emission of the agricultural machine, the carbon emission of the fertilizer, the carbon emission of the pesticide and the carbon emission of farmland cultivation and irrigation to obtain the carbon emission of agricultural management.\|[0110] In the embodiment, carbon emission calculation including the use of agricultural machinery, the use of chemical fertilizers and the application of pesticides in the whole agricultural management process can be realized.\|[0111] On the basis, the farmland carbon emission prediction model for silicate rock weathering comprises the following steps:\|[0112] S=Mp+Fp-Wx-Zx\|[0113] Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|[0114] Specifically, a farmland carbon emission prediction model s=m p+Fp-Wx-Zx based on silicate rock weathering is constructed, and the agricultural production management carbon emission amount is calculated according to the model.\|[0115] Step S103, obtaining a preset farmland carbon emission target value.\|[0116] Specifically, a preset farmland carbon emission target value is set manually, and the preset farmland carbon emission target value is obtained.\|[0117] In this embodiment, a preset target carbon emission value of the farmland is set, and the optimal silicate addition amount and the optimal farmland management measure of the farmland can be determined according to the preset target carbon emission value of the farmland.\|[0118] And step S104, adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount.\|[0119] The farmland management measure adjusting method according to the preset farmland carbon emission target value and the agricultural production management carbon emission comprises the following steps:\|[0120] judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \|[0121] and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|[0122] Specifically, according to the agricultural production management carbon emission calculated by the silicate-weathered farmland carbon emission prediction model, judging whether the agricultural production management carbon emission is greater than a preset farmland carbon emission target value, if not, adjusting the silicate addition amount or changing the addition type and particle size and optimizing farmland management measures.\|[0123] The farmland carbon fixation and collection increasing method based on silicate rock weathering provided by the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after silicate rock carbon fixation and fertilizer increase modifier is added, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for ' carbon peak and ' carbon neutralization ' in the farmland field. Meanwhile, farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and a preset farmland carbon emission target value, and the aim of low carbon emission of agricultural production is achieved.\|[0124] It should be noted that, the method of the embodiment of the present invention may be performed by a single device, for example, a computer or a server. The method of the embodiment can also be applied to a distributed scene, and is completed by mutually matching a plurality of devices. In the case of such a distributed scenario, one of the devices may perform only one or more steps of the method of an embodiment of the present invention, the devices interacting with each other to accomplish the method.\|[0125] It should be noted that the foregoing describes some embodiments of the present invention. Other embodiments are within the scope of the following claims. In some cases, the actions or steps recited in the claims may be performed in a different order than in the embodiments described above and still achieve desirable results. In addition, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In some embodiments, multitasking and parallel processing are also possible or may be advantageous.\|[0126] Based on the same inventive concept, the invention also provides a farmland carbon fixation and exchange increasing system based on silicate rock weathering, which corresponds to the method of any embodiment.\|[0127] Referring to fig. 2, the farmland carbon sequestration and sequestration system based on silicate rock weathering includes:\|[0128] A data acquisition module 201, configured to acquire agricultural management base data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0129] An emissions calculation module 202 for calculating an agricultural production management carbon emissions based on the agricultural management base data; \|[0130] a target obtaining module 203, configured to obtain a preset target value of carbon emission in a farmland; \|[0131] and the management revision module 204 is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount. \|[0132] For convenience of description, the above system is described as being functionally divided into various modules, respectively. Of course, the functions of each module may be implemented in the same piece or pieces of software and/or hardware when implementing the present invention.\|[0133] The system of the above embodiment is used for implementing a corresponding method for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering in any of the foregoing embodiments, and has the beneficial effects of the corresponding method embodiments, which are not described herein.\|[0134] Based on the same inventive concept, the invention also provides equipment corresponding to the method in any embodiment, which comprises a memory, a processor and a computer program stored on the memory and capable of running on the processor, wherein the processor realizes the farmland carbon fixation and exchange increasing method based on silicate rock weathering in any embodiment when executing the program.\|[0135] Fig. 3 shows a more specific hardware architecture of the device provided in this embodiment, where the device may include: a processor 1010, a memory 1020, an input/output interface 1030, a communication interface 1040, and a bus 1050. Wherein processor 1010, memory 1020, input/output interface 1030, and communication interface 1040 implement communication connections therebetween within the device via a bus 1050.\|[0136] The processor 1010 may be implemented by a general-purpose CPU (Central Processing Unit ), a microprocessor, an Application SPECIFIC INTEGRATED Circuit (ASIC), or one or more integrated circuits, etc. for executing related programs to implement the technical solutions provided in the embodiments of the present disclosure.\|[0137] The Memory 1020 may be implemented in the form of ROM (Read Only Memory), RAM (Random Access Memory ), static storage, dynamic storage, etc. Memory 1020 may store an operating system and other application programs, and when the embodiments of the present specification are implemented in software or firmware, the associated program code is stored in memory 1020 and executed by processor 1010.\|[0138] The input/output interface 1030 is used to connect with an input/output module for inputting and outputting information. The input/output module may be configured as a component in a device (not shown) or may be external to the device to provide corresponding functionality. Wherein the input devices may include a keyboard, mouse, touch screen, microphone, various types of sensors, etc., and the output devices may include a display, speaker, vibrator, indicator lights, etc.\|[0139] Communication interface 1040 is used to connect communication modules (not shown) to enable communication interactions of the present device with other devices. The communication module may implement communication through a wired manner (such as USB, network cable, etc.), or may implement communication through a wireless manner (such as mobile network, WIFI, bluetooth, etc.).\|[0140] Bus 1050 includes a path for transferring information between components of the device (e.g., processor 1010, memory 1020, input/output interface 1030, and communication interface 1040).\|[0141] It should be noted that although the above-described device only shows processor 1010, memory 1020, input/output interface 1030, communication interface 1040, and bus 1050, in an implementation, the device may include other components necessary to achieve proper operation. Furthermore, it will be understood by those skilled in the art that the above-described apparatus may include only the components necessary to implement the embodiments of the present description, and not all the components shown in the drawings.\|[0142] The device of the above embodiment is used for implementing a corresponding method for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering in any of the foregoing embodiments, and has the beneficial effects of the corresponding method embodiment, which are not described herein.\|[0143] Those of ordinary skill in the art will appreciate that: the discussion of any of the embodiments above is merely exemplary and is not intended to suggest that the scope of the invention (including the claims) is limited to these examples; the technical features of the above embodiments or in the different embodiments may also be combined within the idea of the invention, the steps may be implemented in any order, and there are many other variations of the different aspects of the embodiments of the invention as described above, which are not provided in detail for the sake of brevity.\|[0144] Any process or method descriptions in flow charts or otherwise described herein may be understood as representing modules, segments, or portions of code which include one or more executable instructions for implementing specific logical functions or steps of the process, and further implementations are included within the scope of the preferred embodiment of the present invention in which functions may be executed out of order from that shown or discussed, including substantially concurrently or in reverse order, depending on the functionality involved, as would be understood by those reasonably skilled in the art of the present invention.\|[0145] Where specific details are set forth in order to describe example embodiments of the invention, it should be apparent to one skilled in the art that embodiments of the invention can be practiced without, or with variation of, these specific details. Accordingly, the description is to be regarded as illustrative in nature and not as restrictive.\|[0146] While the invention has been described in conjunction with specific embodiments thereof, many alternatives, modifications, and variations of those embodiments will be apparent to those skilled in the art in light of the foregoing description.\|[0147] The present embodiments are intended to embrace all such alternatives, modifications and variances which fall within the broad scope of the appended claims. Therefore, any omissions, modifications, equivalent substitutions, improvements, and the like, which are within the spirit and principles of the embodiments of the invention, are intended to be included within the scope of the invention.	(CN118134720)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to a farmland carbon fixation and exchange increase method, system and equipment based on silicate rock weathering.\|BACKGROUND ART\|[0002] With the development of economy, the importance of effective energy utilization, environmental pollution reduction and climate change is increasingly highlighted. The ecological civilization construction of China enters a key period for promoting the synergy of pollution reduction and carbon reduction, promoting the comprehensive green transformation of economic and social development and realizing the change of the quality improvement of ecological environment from variable quantity to variable quality.\|[0003] Enhanced silicate rock weathering is a negative emission technique based on the geochemical principle that aims to accelerate the silicate rock chemical weathering process by adding silicate rock powder to farms or forests to fix more atmospheric CO 2 in a shorter time. The potassium feldspar mineral resources in China are rich, the reserves are huge, the grade is excellent, and a large amount of unutilized mine tailings and alkali silicate waste materials exist, so that the potential of removing the atmospheric CO 2 by enhancing the weathering of silicate rock is huge. At present, a calculation method for carbon emission of soil after silicate rock addition is not available, and a method for carbon fixation and sink increase of soil based on silicate rock weathering is not available.\|DISCLOSURE\|Disclosure of Invention\|[0004] Based on the above, it is necessary to provide a method, a system and a device for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering.\|[0005] A farmland carbon fixation and exchange increase method based on silicate rock weathering comprises the following steps:\|[0006] Acquiring basic agricultural management data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0007] calculating an agricultural production management carbon emission amount according to the agricultural management basic data; \|[0008] acquiring a preset farmland carbon emission target value; \|[0009] And adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|[0010] In one embodiment, calculating the agricultural production management carbon emissions from the agricultural management basis data includes:\|[0011] Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \|[0012] Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \|[0013] obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \|[0014] obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \|[0015] And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|[0016] In one embodiment, the training process for a silicate weathered carbon sink model includes:\|[0017] Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \|[0018] the carbon sink model for the weathering of the preset silicate comprises the following components: \|[0019] Wx=F(x,y,q,d)\|[0020] Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|[0021] In one of the embodiments of the present invention,\|[0022] The training process of the carbon sequestration model for crop planting comprises the following steps:\|[0023] Obtaining carbon planting and sink increasing data according to the farmland environment data; \|[0024] The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \|[0025] wherein, the carbon sequestration model for the preset crop planting comprises: \|[0026] Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\|[0027] Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|[0028] In one embodiment, the training process of the carbon emission model of the soil carbon flux comprises:\|[0029] Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \|[0030] Wherein, the carbon emission model of the preset soil carbon flux comprises: \|[0031] Fp=∑Ti·Ai,ki·ti\|[0032] Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|[0033] In one embodiment, the training process for an agricultural managed carbon emission model includes:\|[0034] The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \|[0035] wherein, the carbon emission model of preset agricultural management includes: \|[0036] Mp=M1+M2+M3+M4\|[0037] M1=∑Al·Ul·αl\|[0038] M2=∑Am·Vm·αm\|[0039] M3=∑An·Wn·αn\|[0040] M4=∑Ao·αo\|[0041] Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|[0042] In one embodiment, a silicate-weathered farmland carbon emission prediction model includes:\|[0043] S=Mp+Fp-Wx-Zx\|[0044] Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|[0045] In one embodiment, adjusting the farmland management measure according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount includes:\|[0046] judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \|[0047] and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|[0048] A farmland carbon sequestration and sequestration system based on silicate rock weathering is used for realizing the farmland carbon sequestration and sequestration method based on silicate rock weathering, and comprises the following steps:\|[0049] the data acquisition module is used for acquiring the agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0050] An emission calculation module for calculating an agricultural production management carbon emission amount according to the agricultural management base data; \|[0051] the target acquisition module is used for acquiring a preset farmland carbon emission target value; \|[0052] And the management revision module is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|[0053] An apparatus comprising a memory, a processor and a computer program stored on the memory and executable on the processor, the processor implementing the steps of a silicate rock weathering based farmland carbon sequestration and sequestration method as described in the various embodiments above when the program is executed.\|[0054] Compared with the prior art, the invention has the advantages that: the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation fertilizer-increasing modifier, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for carbon peak and carbon neutralization in the farmland field. Meanwhile, farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and a preset farmland carbon emission target value, and the aim of low carbon emission of agricultural production is achieved.\|DRAWINGS DESCRIPTION\|[0055] FIG. 1 is a schematic flow diagram of a method for carbon sequestration and sequestration in a farmland based on silicate rock weathering in an embodiment;\|[0056] FIG. 2 is a schematic diagram of a system for carbon sequestration and sequestration in a farmland based on silicate rock weathering in accordance with an embodiment; \|[0057] Fig. 3 is a schematic diagram of the internal structure of the apparatus in one embodiment. \|INVENTION MODE\|Detailed Description\|[0058] Before proceeding with the description of the embodiments of the present invention, the general inventive concept will be described as follows:\|[0059] The invention is mainly developed in the silicate rock farmland improvement process, and at present, a calculation method for carbon emission of soil after silicate rock addition is not available, and a method for carbon fixation and sink enhancement of soil based on silicate rock weathering is not available. \|[0060] Therefore, the invention provides a farmland carbon fixation and collection increasing method based on silicate rock weathering, which comprises the steps of firstly obtaining agriculture management basic data, then calculating the agriculture production management carbon emission according to the agriculture management basic data, and then judging whether to adjust farmland management measures according to the agriculture production management carbon emission and a preset farmland carbon emission target value. The invention realizes quick calculation of farmland carbon emission of different types of farmland soil, silicate rock types, silicate rock addition amount, silicate rock particle size and different cultivation modes, and provides decision support for farmland management.\|[0061] Having described the general inventive concept, the present invention will be further described in detail with reference to the accompanying drawings by way of specific embodiments thereof, in order to make the objects, technical solutions and advantages of the present invention more apparent.\|[0062] It should be noted that unless otherwise defined, technical or scientific terms used in one or more embodiments of the present specification should be given the ordinary meaning as understood by one of ordinary skill in the art to which the present invention pertains. The use of the terms "first," "second," and the like in one or more implementations of the present description does not denote any order, quantity, or importance, but rather the terms "first," "second," and the like are used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that elements or items preceding the word are included in the element or item listed after the word and equivalents thereof, but does not exclude other elements or items. The terms "connected" or "connected," and the like, are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", etc. are used merely to indicate relative positional relationships, which may also be changed when the absolute position of the object to be described is changed.\|[0063] For convenience of understanding, the terms involved in the embodiments of the present invention are explained below:\|[0064] Carbon sink is the process, activity or mechanism of absorbing carbon dioxide in the atmosphere by means of tree planting, vegetation recovery and the like, thereby reducing the concentration of greenhouse gases in the atmosphere. Land ecosystems such as forests, grasslands, wetlands, farmlands, deserts, cities and the like and marine ecosystems are important carbon sinks. \|[0065] Carbon sequestration and sequestration means that the carbon dioxide absorption and storage capacity of an ecosystem are increased by various means and measures, thereby reducing the concentration of carbon dioxide in the atmosphere.\|[0066] In one embodiment, as shown in fig. 1, there is provided a method for carbon sequestration and sequestration in a farmland based on silicate rock weathering, comprising the steps of:\|[0067] Step S101, obtaining agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux, and carbon emission data for agricultural management. \|[0068] Specifically, agricultural management base data is acquired, the agricultural management base data including: carbon sink data based on silicate weathering, farmland environment data based on crop planting, carbon emission data based on soil carbon flux, and carbon emission data based on agricultural management. Wherein the carbon sink data based on silicate weathering comprises: silicate rock type, particle size, precipitation, application amount, weathered carbon sequestration data and the like; the farmland environment data based on crop planting includes: crop growth conditions, climate, weather, air quality, temperature and humidity and the like; carbon emission data based on soil carbon flux includes: carbon flux data, field area data, crop planting time and the like of different crop planting based on exogenous silicate rock addition; carbon emission data based on agricultural management includes: agricultural machine usage data, various kinds of agricultural machine fuel information, agricultural management measure data, and the like.\|[0069] Step S102, calculating the agricultural production management carbon emission amount according to the agricultural management basic data.\|[0070] Specifically, the estimated agricultural production management carbon emission amount can be calculated from the agricultural management base data.\|[0071] On this basis, calculating the agricultural production management carbon emission amount from the agricultural management basis data includes:\|[0072] Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \|[0073] Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \|[0074] obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \|[0075] obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \|[0076] And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|[0077] Specifically, a silicate-weathered carbon sink model based on silicate-weathered silicate is built, a crop-planted carbon sequestration model based on crop planting, a soil carbon flux carbon emission model based on soil respiration and an agricultural management carbon emission model based on agricultural production management are built, a silicate-weathered farmland carbon emission prediction model is built, and the agricultural production management carbon emission amount is obtained through the silicate-weathered farmland carbon emission prediction model.\|[0078] In the embodiment, the carbon emission amount of agricultural production management is calculated by establishing a plurality of models, so that the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation and fertilizer enhancement modifier are solved, the carbon emission amount of agricultural production management can be estimated accurately, and data support is provided for ' carbon peak and ' carbon neutralization ' in the farmland field.\|[0079] On the basis, the training process of the silicate weathered carbon sink model comprises the following steps:\|[0080] Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \|[0081] the carbon sink model for the weathering of the preset silicate comprises the following components: \|[0082] Wx=F(x,y,q,d)\|[0083] Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|[0084] Specifically, a carbon sink model of pre-set silicate weathering based on a random forest algorithm is constructed, W x =f (x, y, q, d). Wherein, F () represents a nonlinear function model of silicate-decomposed carbon sequestration and silicate type, rainfall, silicate application, silicate grain size constructed by random forest algorithm. And training a carbon sink model of the preset silicate weathering through the training data set to obtain the carbon sink model of the silicate weathering which meets the expectations. And acquiring silicate rock type, particle size, precipitation, application amount and weathered carbon fixation data, and calculating the carbon dioxide fixation amount generated by silicate rock weathering, namely the carbon sink amount generated by exogenous silicate rock addition.\|[0085] On the basis, the training process of the carbon sequestration model for crop planting comprises the following steps:\|[0086] Obtaining carbon planting and sink increasing data according to the farmland environment data; \|[0087] The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \|[0088] wherein, the carbon sequestration model for the preset crop planting comprises: \|[0089] Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\|[0090] Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|[0091] Specifically, farmland environment data are obtained, and carbon planting and collection increasing data of a target area are obtained through the existing identification model. Wherein, the carbon planting and sink increasing data comprises: crop type information and plant type information, crop weight information, moisture content of harvested part of crops, root cap ratio of crops and economic coefficient of crops.\|[0092] And constructing a carbon sequestration model Z x=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi for the preset crop planting based on the crop planting, training the carbon sequestration model for the preset crop planting through a training data set to obtain a carbon sequestration model which accords with the expected crop planting, and calculating the carbon sequestration amount generated by the crop growth according to the carbon sequestration data.\|[0093] On the basis, the training process of the carbon emission model of the soil carbon flux comprises the following steps:\|[0094] Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \|[0095] Wherein, the carbon emission model of the preset soil carbon flux comprises: \|[0096] Fp=∑Ti·Ai,ki·ti\|[0097] Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|[0098] Specifically, a multiple regression relation between measured carbon flux data and crop planting types and soil textures is constructed, a carbon emission model of the preset soil carbon flux based on the crop types and the soil textures is determined, F p=∑Ti·Ai,ki·ti, and training of the carbon emission model of the preset soil carbon flux is carried out through a training data set, so that a carbon emission model which accords with expected soil carbon flux is obtained. And obtaining carbon flux data, field area data and crop planting time based on different crop planting of exogenous silicate rock addition, and calculating to obtain the carbon emission of the soil.\|[0099] In the embodiment, based on the BP neural network, a multiple regression relation between actually measured exogenous silicate rock added carbon flux data and crop planting types and soil textures is constructed, and the automatic calculation of the carbon emission of the soil can be realized by operating the constructed carbon emission model of the soil carbon flux.\|[0100] On this basis, the training process of the carbon emission model of agricultural management comprises the following steps:\|[0101] The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \|[0102] wherein, the carbon emission model of preset agricultural management includes: \|[0103] Mp=M1+M2+M3+M4\|[0104] M1=∑Al·Ul·αl\|[0105] M2=∑Am·Vm·αm\|[0106] M3=∑An·Wn·αn\|[0107] M4=∑Ao·αo\|[0108] Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|[0109] Specifically, the use data of the agricultural machine is obtained, the agricultural management carbon emission is calculated by combining the agricultural management measure data, and the agricultural production carbon emission information is obtained. Various agricultural machine usage data include: fuel oil information of various kinds of agricultural machines, time length information of various kinds of agricultural machines, power information of various kinds of agricultural machines, and use quantity information of various kinds of agricultural machines; acquiring carbon emission factor information of various fuels based on the fuel information of various agricultural machines, and multiplying the carbon emission factor information of various fuels, the power information of various agricultural machines, the time-length information of various agricultural machines and the use quantity information of various agricultural machines to obtain the carbon emission quantity of the agricultural machines; obtaining chemical fertilizer use information and pesticide use information according to the agricultural management measure data, obtaining chemical fertilizer carbon emission factor information of various types and pesticide carbon emission factor information of various types based on the chemical fertilizer use information and the pesticide use information, calculating the product of the chemical fertilizer use information and the carbon emission factor of the corresponding chemical fertilizer type as chemical fertilizer carbon emission amount, and calculating the product of the pesticide use information and the carbon emission factor of the corresponding pesticide type as pesticide carbon emission amount; calculating the product of the cultivation and irrigation use information and the carbon emission factors of the corresponding modes as the carbon emission amount of farmland cultivation and irrigation; and combining the carbon emission of the agricultural machine, the carbon emission of the fertilizer, the carbon emission of the pesticide and the carbon emission of farmland cultivation and irrigation to obtain the carbon emission of agricultural management.\|[0110] In the embodiment, carbon emission calculation including the use of agricultural machinery, the use of chemical fertilizers and the application of pesticides in the whole agricultural management process can be realized.\|[0111] On the basis, the farmland carbon emission prediction model for silicate rock weathering comprises the following steps:\|[0112] S=Mp+Fp-Wx-Zx\|[0113] Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|[0114] Specifically, a farmland carbon emission prediction model s=m p+Fp-Wx-Zx based on silicate rock weathering is constructed, and the agricultural production management carbon emission amount is calculated according to the model.\|[0115] Step S103, obtaining a preset farmland carbon emission target value.\|[0116] Specifically, a preset farmland carbon emission target value is set manually, and the preset farmland carbon emission target value is obtained.\|[0117] In this embodiment, a preset target carbon emission value of the farmland is set, and the optimal silicate addition amount and the optimal farmland management measure of the farmland can be determined according to the preset target carbon emission value of the farmland.\|[0118] And step S104, adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount.\|[0119] The farmland management measure adjusting method according to the preset farmland carbon emission target value and the agricultural production management carbon emission comprises the following steps:\|[0120] judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \|[0121] and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|[0122] Specifically, according to the agricultural production management carbon emission calculated by the silicate-weathered farmland carbon emission prediction model, judging whether the agricultural production management carbon emission is greater than a preset farmland carbon emission target value, if not, adjusting the silicate addition amount or changing the addition type and particle size and optimizing farmland management measures.\|[0123] The farmland carbon fixation and collection increasing method based on silicate rock weathering provided by the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after silicate rock carbon fixation and fertilizer increase modifier is added, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for ' carbon peak and ' carbon neutralization ' in the farmland field. Meanwhile, farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and a preset farmland carbon emission target value, and the aim of low carbon emission of agricultural production is achieved.\|[0124] It should be noted that, the method of the embodiment of the present invention may be performed by a single device, for example, a computer or a server. The method of the embodiment can also be applied to a distributed scene, and is completed by mutually matching a plurality of devices. In the case of such a distributed scenario, one of the devices may perform only one or more steps of the method of an embodiment of the present invention, the devices interacting with each other to accomplish the method.\|[0125] It should be noted that the foregoing describes some embodiments of the present invention. Other embodiments are within the scope of the following claims. In some cases, the actions or steps recited in the claims may be performed in a different order than in the embodiments described above and still achieve desirable results. In addition, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In some embodiments, multitasking and parallel processing are also possible or may be advantageous.\|[0126] Based on the same inventive concept, the invention also provides a farmland carbon fixation and exchange increasing system based on silicate rock weathering, which corresponds to the method of any embodiment.\|[0127] Referring to fig. 2, the farmland carbon sequestration and sequestration system based on silicate rock weathering includes:\|[0128] A data acquisition module 201, configured to acquire agricultural management base data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0129] An emissions calculation module 202 for calculating an agricultural production management carbon emissions based on the agricultural management base data; \|[0130] a target obtaining module 203, configured to obtain a preset target value of carbon emission in a farmland; \|[0131] and the management revision module 204 is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount. \|[0132] For convenience of description, the above system is described as being functionally divided into various modules, respectively. Of course, the functions of each module may be implemented in the same piece or pieces of software and/or hardware when implementing the present invention.\|[0133] The system of the above embodiment is used for implementing a corresponding method for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering in any of the foregoing embodiments, and has the beneficial effects of the corresponding method embodiments, which are not described herein.\|[0134] Based on the same inventive concept, the invention also provides equipment corresponding to the method in any embodiment, which comprises a memory, a processor and a computer program stored on the memory and capable of running on the processor, wherein the processor realizes the farmland carbon fixation and exchange increasing method based on silicate rock weathering in any embodiment when executing the program.\|[0135] Fig. 3 shows a more specific hardware architecture of the device provided in this embodiment, where the device may include: a processor 1010, a memory 1020, an input/output interface 1030, a communication interface 1040, and a bus 1050. Wherein processor 1010, memory 1020, input/output interface 1030, and communication interface 1040 implement communication connections therebetween within the device via a bus 1050.\|[0136] The processor 1010 may be implemented by a general-purpose CPU (Central Processing Unit ), a microprocessor, an Application SPECIFIC INTEGRATED Circuit (ASIC), or one or more integrated circuits, etc. for executing related programs to implement the technical solutions provided in the embodiments of the present disclosure.\|[0137] The Memory 1020 may be implemented in the form of ROM (Read Only Memory), RAM (Random Access Memory ), static storage, dynamic storage, etc. Memory 1020 may store an operating system and other application programs, and when the embodiments of the present specification are implemented in software or firmware, the associated program code is stored in memory 1020 and executed by processor 1010.\|[0138] The input/output interface 1030 is used to connect with an input/output module for inputting and outputting information. The input/output module may be configured as a component in a device (not shown) or may be external to the device to provide corresponding functionality. Wherein the input devices may include a keyboard, mouse, touch screen, microphone, various types of sensors, etc., and the output devices may include a display, speaker, vibrator, indicator lights, etc.\|[0139] Communication interface 1040 is used to connect communication modules (not shown) to enable communication interactions of the present device with other devices. The communication module may implement communication through a wired manner (such as USB, network cable, etc.), or may implement communication through a wireless manner (such as mobile network, WIFI, bluetooth, etc.).\|[0140] Bus 1050 includes a path for transferring information between components of the device (e.g., processor 1010, memory 1020, input/output interface 1030, and communication interface 1040).\|[0141] It should be noted that although the above-described device only shows processor 1010, memory 1020, input/output interface 1030, communication interface 1040, and bus 1050, in an implementation, the device may include other components necessary to achieve proper operation. Furthermore, it will be understood by those skilled in the art that the above-described apparatus may include only the components necessary to implement the embodiments of the present description, and not all the components shown in the drawings.\|[0142] The device of the above embodiment is used for implementing a corresponding method for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering in any of the foregoing embodiments, and has the beneficial effects of the corresponding method embodiment, which are not described herein.\|[0143] Those of ordinary skill in the art will appreciate that: the discussion of any of the embodiments above is merely exemplary and is not intended to suggest that the scope of the invention (including the claims) is limited to these examples; the technical features of the above embodiments or in the different embodiments may also be combined within the idea of the invention, the steps may be implemented in any order, and there are many other variations of the different aspects of the embodiments of the invention as described above, which are not provided in detail for the sake of brevity.\|[0144] Any process or method descriptions in flow charts or otherwise described herein may be understood as representing modules, segments, or portions of code which include one or more executable instructions for implementing specific logical functions or steps of the process, and further implementations are included within the scope of the preferred embodiment of the present invention in which functions may be executed out of order from that shown or discussed, including substantially concurrently or in reverse order, depending on the functionality involved, as would be understood by those reasonably skilled in the art of the present invention.\|[0145] Where specific details are set forth in order to describe example embodiments of the invention, it should be apparent to one skilled in the art that embodiments of the invention can be practiced without, or with variation of, these specific details. Accordingly, the description is to be regarded as illustrative in nature and not as restrictive.\|[0146] While the invention has been described in conjunction with specific embodiments thereof, many alternatives, modifications, and variations of those embodiments will be apparent to those skilled in the art in light of the foregoing description.\|[0147] The present embodiments are intended to embrace all such alternatives, modifications and variances which fall within the broad scope of the appended claims. Therefore, any omissions, modifications, equivalent substitutions, improvements, and the like, which are within the spirit and principles of the embodiments of the invention, are intended to be included within the scope of the invention.	Family Number\|(110028832)\|110028832\|Object of Invention\|(CN118134720 A)\|The invention provides a method , a system and equipment for carbon fixation and sink enhancement of farmland based on silicate rock weathering , wherein the method comprises the following steps : acquiring basic agricultural management data ; wherein , the agricultural management base data includes : carbon sequestration data for silicate weathering , farmland environment data , carbon emission data for soil carbon flux and carbon emission data for agricultural management ; calculating an agricultural production management carbon emission amount according to the ( . . . ) \|The invention relates to a farmland carbon fixation and exchange increase method , system and equipment based on silicate rock weathering .\|Therefore , the invention provides a farmland carbon fixation and collection increasing method based on silicate rock weathering , which comprises the steps of firstly obtaining agriculture management basic data , then calculating the agriculture production management carbon emission according to the agriculture management basic data , and then judging whether to adjust ( . . . ) \|Abstract\|(CN118134720 A)\|The invention provides a farmland carbon sequestration and sink increase method , system and equipment based on silicate rock weathering , and the method comprises the steps : obtaining agricultural management basic data ; wherein the agricultural management basic data comprises silicate weathering carbon sink data , farmland environment data , soil carbon flux carbon emission data and agricultural management carbon emission data ; calculating agricultural production management carbon emission according to the agricultural management basic data ; acquiring a preset farmland carbon emission target value ; and adjusting farmland management measures according to a preset farmland carbon emission target value and the agricultural production management carbon emission . According to the method , the agricultural production management carbon emission can be calculated , the problem that the farmland carbon emission is unknown after the silicate rock - based carbon sequestration and fertility improvement agent is added is solved , the agricultural production management carbon emission can be accurately estimated , and data support is provided for achieving the carbon emission target . Farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and the preset farmland carbon emission target value . \|Title\|(CN118134720 A)\|Farmland carbon sequestration and sink increase method , system and equipment based on silicate rock weathering \|Advantages / Prev. Drawbacks\|(CN118134720 A)\|( . . . ) invention has the advantages that : the invention can calculate the carbon emission amount of agricultural production management , solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock - based carbon fixation fertilizer - increasing modifier , can accurately estimate the carbon emission amount of agricultural production management , and provides data support for carbon peak and carbon neutralization in the farmland field . \|Independent Claims\|(CN118134720 A)\|1. A farmland carbon fixation and sink enhancement method based on silicate rock weathering is characterized by comprising the following steps : Acquiring basic agricultural management data ; wherein the agricultural management base data includes : carbon sequestration data for silicate weathering , farmland environment data , carbon emission data for soil carbon flux and carbon emission data for agricultural management ; calculating an agricultural production management carbon emission amount according to the ( . . . ) \|	IT methods for management	G06N-003/08/4\|G06N-005/02/5\|G06N-005/04/1\|G06Q-010/06/3\|G06Q-050/02\|G06Q-050/26\|Y02A-090/10		G06N-003/08/4\|G06N-005/02/5\|G06N-005/04/1\|G06Q-010/06/3\|G06Q-050/02\|G06Q-050/26\|Y02A-090/10	G06N-003/084\|G06N-005/025\|G06N-005/04\|G06Q-010/063\|G06Q-050/02\|G06Q-050/26	G06N-003/084\|G06N-005/025\|G06N-005/04\|G06Q-010/063\|G06Q-050/02\|G06Q-050/26			CN120893778\|CN120450211	CN120893778 116542026 WHO=Examiner SELF=N CAT=A\|CN120450211 115573877 WHO=Examiner SELF=N CAT=A						PENDING	(CN118134720)\|PENDING	ALIVE	(CN118134720)\|ALIVE	(CN118134720)\|LEGAL DETAILS FOR CN118134720\|Actual or expected expiration date=2044-02-06\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-02-06\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202410172022\|Application date=2024-02-06\|Standardized application number=2024CN-0172022\|Event publication date=2024-06-04\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN118134720\|Publication stage code=A\|Publication date=2024-06-04\|Standardized publication number=CN118134720\|Event publication date=2024-06-04\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2024-06-21\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN118134720)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoROL0nYw6nBn1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000073002387&ekey=2254&xpn=CN118134720&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=piYDbYyO4oSmOEdPZfo6iZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN118134720)\|CN	(CN118134720)\|NAME=CHONGQING INSTITUTE OF GEOLOGY AND MINERAL RESOURCES , COUNTRY=CN		(CN118134720)\|NAME=YU HONG;CHONGQING ZHI HUI ZHI YUAN INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=50234		(CN118134720)\|NAME=MA LEI\|NAME=SI HONGTAO\|NAME=MAO ZHENG\|NAME=WANG CHEN\|NAME=LI CHENG\|NAME=XU MINGZE\|NAME=ZHU DONGXUE\|NAME=ZHU DAN\|NAME=XU WENXING	(CN118134720)\|3	1	1					(CN118134720)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2024-06-04\|Gazette number: GAZNUM=40-2301\|Number of Pages: NPAGES=15\|		(CN118134720)\|CHINESE (CHI)	(CN118134720)\|Patent	Titre: (CN118134720)\|Farmland carbon sequestration and sink increase method, system and equipment based on silicate rock weathering Résumé: (CN118134720)\|The invention provides a farmland carbon sequestration and sink increase method, system and equipment based on silicate rock weathering, and the method comprises the steps: obtaining agricultural management basic data; wherein the agricultural management basic data comprises silicate weathering carbon sink data, farmland environment data, soil carbon flux carbon emission data and agricultural management carbon emission data; calculating agricultural production management carbon emission according to the agricultural management basic data; acquiring a preset farmland carbon emission target value; and adjusting farmland management measures according to a preset farmland carbon emission target value and the agricultural production management carbon emission. According to the method, the agricultural production management carbon emission can be calculated, the problem that the farmland carbon emission is unknown after the silicate rock-based carbon sequestration and fertility improvement agent is added is solved, the agricultural production management carbon emission can be accurately estimated, and data support is provided for achieving the carbon emission target. Farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and the preset farmland carbon emission target value.	0	Abstract	gpt-4o-mini	yes	The article discusses a method for carbon sequestration based on silicate rock weathering, which aligns with the topic of enhanced weathering for CO₂ capture and storage.
9	receiving an input liquid comprising at least one of seawater	brackish water	and brine effluent;																																																																			Titre: nan Résumé: nan	15		gpt-4o-mini	uncertain	No usable text found.	empty_text
10	performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream;																																																																					Titre: nan Résumé: nan	16		gpt-4o-mini	uncertain	No usable text found.	empty_text
11	CN202210271537	CN202310250007\|CN202210271537	CN116463001\|CN116463001\|CN114574045	100341084	CN116463001 B 2024-07-05 [CN116463001B]\|CN116463001 A 2023-07-21 [CN116463001]\|CN114574045 A 2022-06-03 [CN114574045]	2022-03-18	2023-03-15\|2022-03-18	2024-07-05\|2023-07-21\|2022-06-03	(CN116463001B)\|2024-07-05\|	(CN116463001)\|2043-03-15\|(CN114574045)\|2023-08-29	(CN116463001)\|Water medium carbon dioxide capturing surface layer coating and preparation method thereof	(CN116463001)\|The invention discloses a water medium carbon dioxide capture surface coating and a preparation method thereof. The water medium carbon dioxide capture surface coating is formed by mixing polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, kieselguhr, calcium silicate, rock wool fibers and thin cement paste according to a certain mass ratio. The mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the coating is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; and the mass ratio of the thin cement paste in the coating is 35-57%. The coating is smeared on the surface of a building, and when a coating layer is dry, carbon dioxide can be automatically captured from air; when the coating layer is wet, the coating layer can desorb carbon dioxide and dissolve the carbon dioxide in water in a carbonate form to flow out, so that the carbon breathing function of the external facade of the building is realized.	DONGHUA UNIVERSITY\|SHANGHAI ZEYAO ENV PROT TECHNOLOGY	(CN116463001)\|SHANGHAI ZEYAO ENV PROT TECH CO LTD ([CN])\|DONGHUA UNIVERSITY\|(CN116463001)\|SHANGHAI ZEYAO ENV PROT TECH CO LTD ([CN])\|DONGHUA UNIVERSITY\|(CN114574045)\|SHANGHAI ZEYAO ENV PROT TECH CO LTD ([CN])\|DONGHUA UNIVERSITY	SONG XINSHAN\|XU YONG\|ZHANG ZHILAN\|WANG YUHUI\|XU ZHONGSHUO\|WANG YIFEI\|LIU YINGYING\|TAN SHUJUAN\|HUANG NA\|TANG HAIYAN	(CN116463001)\|Song Xinshan\|Xu Yong\|Zhang Zhilan\|Wang Yuhui\|Xu Zhongshuo\|Wang Yifei\|Liu Yingying\|Tan Shujuan\|Huang Na\|Tang Haiyan\|(CN116463001)\|SONG XINSHAN\|XU YONG\|ZHANG ZHILAN\|WANG YUHUI\|XU ZHONGSHUO\|WANG YIFEI\|LIU YINGYING\|TAN SHUJUAN\|HUANG NA\|TANG HAIYAN	(CN116463001)\|XU HAOJUN;SHANGHAI JIANQIU INTELLECTUAL PROPERTY ATTORNEYS\|Reg. Nb: 31382\|(CN114574045)\|HE XINXIN;Hefei Du Lei Intellectual Property Agency (General Partnership)\|Reg. Nb: 34227	(CN116463001)\|In practice, however, there are a number of substances that can achieve carbon dioxide adsorption, but it is difficult to achieve regeneration under normal environmental conditions (condition (4) is not satisfied), because they must overcome a large energy barrier to regenerate.\|	(CN116463001)\|1. The preparation method of the water medium carbon dioxide capturing surface layer coating is characterized by comprising polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion; Wherein the mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%; the hydrotalcite-like mineral is layered double metal hydroxide formed by Ca/Al/Mg metal oxide, is from natural hydrohead mineral, is assembled by positively charged octahedral main body laminates and interlayer anions through non-covalent bond interaction, and has the particle size range of 0.1-1.0mm; the paint is applied to the surface of a building, carbon dioxide can be automatically captured from the air when the paint layer is dry, and the paint layer can desorb the carbon dioxide and dissolve in water in the form of carbonate to flow out when the paint layer is wet. \|	(CN116463001)\|The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried; when the air is wet, carbon dioxide in the gaps of the coating layer is converted into carbonate or bicarbonate to be released, and the carbonate or bicarbonate is flushed with water to enter the water body, so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled, and the problems in the background art are solved. In order to achieve the above purpose, the present invention provides the following technical solutions:\|The invention discloses a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the coating is composed of polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion; the mass ratio of the polystyrene quaternary ammonium salt resin in the paint is 10-15%; the mass ratio of hydrotalcite-like minerals in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the paint is 17-25%; the mass ratio of the rock wool fiber in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%.\|The invention relates to the technical field of carbon capture, in particular to a water-medium carbon dioxide capture surface layer coating and a preparation method thereof.\|	(CN116463001)\|CARBON DIOXIDE(100,61)\|HYDROTALCITE MINERAL(100,25)\|COATING LAYER(100,19)\|WATER MEDIUM(100,8)\|WATER MEDIUM CARBON DIOXIDE(100,8)\|MEDIUM CARBON DIOXIDE(100,2)\|SURFACE LAYER COATING(100,2)\|QUATERNARY AMMONIUM SALT RESIN(80,22)\|ROCK WOOL FIBER(79,11)\|NATURAL HYDROHEAD MINERAL(66,1)\|AMMONIUM SALT RESIN(62,22)\|PAINT LAYER(62,6)\|PAINT(55,17)\|CEMENT SLURRY(53,10)\|NONCOVALENT BOND INTERACTION(49,3)\|WOOL FIBER(47,14)\|SALT RESIN(46,22)\|POLYSTYRENE(42,28)\|INTERLAYER ANION(41,3)\|DIATOMITE(38,16)\|OCTAHEDRAL MAIN BODY LAMINATE(36,1)\|DIATOMITE MASS RATIO(35,3)\|CALCIUM SILICATE(34,23)\|BICARBONATE(32,2)\|MASS RATIO(30,29)\|CARBON DIOXIDE CAPTURE(30,4)\|HYDROTALCITE MINERAL MASS RATIO(30,2)\|BONDING INTERACTION(28,3)\|LAMINATING BODY(28,1)\|CARBON DIOXIDE ADSORPTION(26,1)\|REGENERATION(24,1)\|SPRAY FUNCTIONAL COATING(24,1)\|COATING LAYER GAP(23,1)\|LAYERED DOUBLE METAL HYDROXIDE(20,3)\|WATERBORNE(18,1)\|CALCIUM SILICATE PARTICLE(17,4)\|LAYERED DOUBLE METAL(17,3)\|WATER CARBON DIOXIDE(16,3)\|CARBON CAPTURE(13,1)\|STRUCTURE OUTER FACADE(12,1)\|CAPTURING SURFACE LAYER(11,4)\|CARBON RESPIRATION(11,2)\|DIATOMITE PARTICLE(10,3)\|INTENSIVE QUATERNIZATION(10,2)\|PARTICLE SIZE(9,16)\|DIRECTLY SMEARED COATING(9,3)\|MG METAL OXIDE(9,3)\|POWDER SHAPE(9,3)\|ENVIRONMENTAL CONDITION(9,2)\|LARGE ENERGY BARRIER(9,1)\|AMMONIUM SALT(8,8)\|CHLORO METHYL POLYSTYRENE(8,2)\|WATER BODY(8,2)\|HYDROTALCITE MINERAL PARTICLE(8,1)\|MAGNESIA OCTAHEDRON(8,1)\|NATURAL HYDROHEAD ORE(8,1)\|OCTAHEDRAL HOST LAMINATE(8,1)\|CA AL(7,3)\|BUILDING OUTER FACADE(7,2)\|POLYSTYRENE RESIN POWDER PARTICLE(7,2)\|COATING MILDEW PREVENTION(7,1)\|INFRARED GAS ANALYZER LICOR(7,1)\|JINING SANSHI BIOTECHNOLOGY CO(7,1)\|NATURAL HYDROTALCITE MINERAL(7,1)\|OBSERVATION INSTRUMENT(7,1)\|ALUMINA OCTAHEDRON(6,1)\|AMINE ADSORBENT(6,1)\|PREPARED SURFACE COATING(6,1)\|TECHNICAL FEATURE(5,3)\|ALUMINUM MAGNESIUM HYDROTALCITE(5,2)\|FLAME RETARDANCE FUNCTION(5,2)\|POLYETHYLENIMINE(5,2)\|QUATERNARY AMMONIUM ION EXCHANGE(5,2)\|NATURAL HYDROFLUORITE(5,1)\|SOAKING(4,4)\|ANTIBIOSIS(4,2)\|BROMOBUTANE(4,2)\|BROMODODECANE(4,2)\|CARBON DIOXIDE ABSORPTION(4,2)\|ISOPROPANOL(4,2)\|PRESERVATION(4,2)\|SAMPLE CELL(4,2)\|SAMPLE CHAMBER(4,2)\|ALUMINUM CALCIUM HYDROTALCITE(4,1)\|BICARBONATE FORMATION(4,1)\|CONTRADICTION(4,1)\|DISPERSING MACHINE(4,1)\|DRIED TILE(4,1)\|HYDROTALCITE MINERAL SCHEMATIC DIAGRAM(4,1)\|INORGANIC PARTICLE(4,1)\|MASS SHARE(4,1)\|MILDEW PROOF(4,1)\|MILDEW RESISTANCE(4,1)\|PREMIXING(4,1)\|RAPID REGENERATION(4,1)\|WATER VAPOR COMPETITIVE ADSORPTION(4,1)\|HCO(3,3)\|ADSORPTION DESORPTION(3,1)\|BEAKER(3,1)\|BICARBONATE ANION(3,1)\|\|(CN116463001)\|CARBON DIOXIDE(100,64)\|HYDROTALCITE MINERAL(100,26)\|COATING LAYER(100,20)\|WATER MEDIUM(100,9)\|WATER MEDIUM CARBON DIOXIDE(100,9)\|MEDIUM CARBON DIOXIDE(100,2)\|SURFACE LAYER COATING(100,2)\|QUATERNARY AMMONIUM SALT RESIN(96,25)\|ROCK WOOL FIBER(90,12)\|AMMONIUM SALT RESIN(75,25)\|PAINT(57,18)\|CEMENT SLURRY(56,10)\|SALT RESIN(55,25)\|WOOL FIBER(54,15)\|POLYSTYRENE(50,30)\|DIATOMITE(42,17)\|DIATOMITE MASS RATIO(42,4)\|CALCIUM SILICATE(40,25)\|NATURAL HYDROTALC ORE(39,1)\|MASS RATIO(36,36)\|OCTAHEDRAL HOST LAMINATE(36,2)\|NONCOVALENT INTERACTION(34,1)\|PAINT LAYER(32,3)\|INTENSIVE QUATERNIZATION(29,3)\|WATERBORNE CARBON DIOXIDE(29,2)\|HYDROTALCITE MINERAL MASS RATIO(28,2)\|CARBON DIOXIDE CAPTURE(27,5)\|BICARBONATE(27,3)\|INTERLAYER ANION(25,3)\|CHLORO METHYL POLYSTYRENE(24,3)\|CARBON DIOXIDE ADSORPTION(24,1)\|REGENERATION(22,1)\|POLYSTYRENE RESIN POWDER PARTICLE(21,3)\|COATING LAYER GAP(21,1)\|WATER CARBON DIOXIDE(17,4)\|CALCIUM SILICATE PARTICLE(16,4)\|POLYETHYLENIMINE(16,3)\|SOAKING(14,6)\|BROMODODECANE(14,3)\|BROMOBUTANE(13,3)\|CAPTURING SURFACE LAYER(12,5)\|ISOPROPANOL(12,3)\|LAYERED DOUBLE METAL HYDROXIDE(12,3)\|CARBON CAPTURE(12,1)\|CARBON RESPIRATION(11,2)\|STRUCTURE OUTER FACADE(11,1)\|DIATOMITE PARTICLE(10,3)\|SWELLING(10,3)\|POWDER SHAPE(9,3)\|ENVIRONMENTAL CONDITION(9,2)\|NONCOVALENT BOND INTERACTION(9,2)\|WATER BODY(8,2)\|LARGE ENERGY BARRIER(8,1)\|PARTICLE SIZE(7,16)\|BUILDING OUTER FACADE(7,2)\|HYDROTALCITE MINERAL PARTICLE(7,1)\|MAGNESIA OCTAHEDRON(7,1)\|NATURAL HYDROHEAD ORE(7,1)\|COATING MILDEW PREVENTION(6,1)\|INFRARED GAS ANALYZER LICOR(6,1)\|JINING SANSHI BIOTECHNOLOGY CO(6,1)\|NATURAL HYDROTALCITE MINERAL(6,1)\|OBSERVATION INSTRUMENT(6,1)\|MG METAL OXIDE(5,3)\|TECHNICAL FEATURE(5,3)\|ALUMINUM MAGNESIUM HYDROTALCITE(5,2)\|BONDING INTERACTION(5,2)\|FLAME RETARDANCE FUNCTION(5,2)\|ALUMINA OCTAHEDRON(5,1)\|PREPARED SURFACE COATING(5,1)\|CA AL(4,3)\|ROOM TEMPERATURE(4,3)\|ANTIBIOSIS(4,2)\|CARBON DIOXIDE ABSORPTION(4,2)\|PRESERVATION(4,2)\|SAMPLE CELL(4,2)\|SAMPLE CHAMBER(4,2)\|NATURAL HYDROFLUORITE(4,1)\|ALUMINUM CALCIUM HYDROTALCITE(3,1)\|BICARBONATE FORMATION(3,1)\|CLOSED PLEXIGLASS(3,1)\|CONTRADICTION(3,1)\|DISPERSING MACHINE(3,1)\|DRIED TILE(3,1)\|HYDROTALCITE MINERAL SCHEMATIC DIAGRAM(3,1)\|INORGANIC PARTICLE(3,1)\|MASS SHARE(3,1)\|MILDEW PROOF(3,1)\|MILDEW RESISTANCE(3,1)\|POLYSTYRENETHE CARBON DIOXIDE(3,1)\|PREMIXING(3,1)\|RAPID REGENERATION(3,1)\|\|(CN114574045)\|CARBON DIOXIDE(100,64)\|WATERBORNE CARBON DIOXIDE(100,15)\|COATING SURFACE(100,6)\|HYDROTALCITE MINERAL(97,21)\|ROCK WOOL FIBER(82,18)\|QUATERNARY AMMONIUM SALT RESIN(77,22)\|CCS ALONE2THE STABILITY(72,1)\|CEMENT SLURRY(70,8)\|AMMONIUM SALT RESIN(60,22)\|WOOL FIBER(51,8)\|CARBON DIOXIDE CAPTURE TOPCOAT(49,3)\|DIATOMITE(47,16)\|COATING LAYER(47,15)\|AUTOMATIC CAPTURE(46,3)\|SALT RESIN(44,22)\|POLYSTYRENE(41,29)\|NONCOVALENT BOND INTERACTION(37,3)\|CALCIUM SILICATE(31,19)\|DIATOMITE PARTICLE(29,4)\|INTERLAYER ANION(29,3)\|WATERBORNE CARBON DIOXIDE CAPTURE(27,2)\|REGENERATION(26,1)\|ENHANCED QUATERNIZATION(25,3)\|POLYSTYRENE RESIN POWDER PARTICLE(25,3)\|BICARBONATE(25,1)\|COATING LAYER GAP(25,1)\|DIFFICULT TASK(25,1)\|OCTAHEDRAL MAIN(25,1)\|NATURAL HYDROTALCITE(24,4)\|CARBON DIOXIDE AUTOMATIC CAPTURE(23,2)\|OUTER FACADE(23,2)\|CARBON DIOXIDE ADSORPTION(22,2)\|FOSSIL FUEL(21,1)\|GLOBAL WARMING PREVENTION(21,1)\|SPRAYING(19,4)\|ENERGY INFRASTRUCTURE(19,1)\|CALCIUM SILICATE PARTICLE(18,4)\|POLYETHYLENEIMINE(18,3)\|ANTIFUNGAL FUNCTION(17,1)\|SOAKING(16,7)\|MIXING RATIO MASS(16,5)\|ANTIBACTERIAL(16,2)\|WATER MEDIUM(16,1)\|COATING FUNCTION(15,3)\|PRESERVATION(15,3)\|FLAME RETARDANT(14,2)\|CARBON CAPTURE(14,1)\|MASS RATIO(13,18)\|ISOPROPANOL(13,3)\|STRUCTURE OUTER FACADE(13,2)\|COATING VOID RATIO(11,3)\|SWELLING(11,3)\|MIXING RATIO(10,5)\|POWDER SHAPE(10,3)\|ENVIRONMENTAL CONDITION(10,2)\|LARGE ENERGY BARRIER(10,1)\|WATER BODY(9,2)\|CO2AMINE SORBENT(9,1)\|HYDROTALCITE MINERAL PARTICLE(9,1)\|DIRECTLY COATED COATING(8,3)\|COATING MILDEW PREVENTION(8,1)\|COMPETITIVE ADSORPTION(8,1)\|INFRARED GAS ANALYZER LICOR(8,1)\|OBSERVATION INSTRUMENT(8,1)\|RENEWABLE ENERGY SOURCE(8,1)\|MASS FRACTION(7,3)\|HEAT INSULATION(7,2)\|SAMPLE CHAMBER(6,4)\|AQUEOUS MEDIUM(6,2)\|BONDING INTERACTION(6,2)\|BUILDING OUTER VERTICAL SURFACE(6,1)\|CREATIVE EFFORT(6,1)\|MILDEW PROOF(6,1)\|OCTAHEDRAL HOST(6,1)\|TRANSITION PERIOD2CAPTURE(6,1)\|CA AL(5,3)\|GAS EXCHANGE(5,3)\|MG METAL OXIDE(5,3)\|BICARBONATE RADICAL FORMATION(5,1)\|LAYERED DOUBLE HYDROXIDE(5,1)\|OUTER VERTICAL SURFACE(5,1)\|RAPID REGENERATION(5,1)\|SURFACE LAYER(5,1)\|HCO(4,4)\|ROOM TEMPERATURE(4,3)\|TILE(4,3)\|AIR2ABSORPTION(4,1)\|CAPTURE RELEASE CIRCULATION(4,1)\|CLOSED PLEXIGLASS CHAMBER(4,1)\|CO2A CAPTURE RELEASE CYCLE(4,1)\|DISPERSION MACHINE(4,1)\|FLAME RETARDANCE FUNCTION(4,1)\|HANDTHE(4,1)\|INORGANIC PARTICLE(4,1)\|MOISTURE BOUND(4,1)\|PARTICLE SIZE RANGE(4,1)\|	(CN116463001)\|1. The preparation method of the water medium carbon dioxide capturing surface layer coating is characterized by comprising polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion;\| Wherein the mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%; \| the hydrotalcite-like mineral is layered double metal hydroxide formed by Ca/Al/Mg metal oxide, is from natural hydrohead mineral, is assembled by positively charged octahedral main body laminates and interlayer anions through non-covalent bond interaction, and has the particle size range of 0.1-1.0mm; \| the paint is applied to the surface of a building, carbon dioxide can be automatically captured from the air when the paint layer is dry, and the paint layer can desorb the carbon dioxide and dissolve in water in the form of carbonate to flow out when the paint layer is wet. \|2. The method for preparing the water-based carbon dioxide capturing surface layer paint according to claim 1, wherein the polystyrene quaternary ammonium salt resin adopts commercial powder particles with the particle size of 0.2-1.0mm.\|3. The method for preparing the water-based carbon dioxide capturing surface layer paint according to claim 1, wherein the diatomite is in a powder shape and has a particle size of 0.5-1.0mm.\|4. The method for preparing the water-borne carbon dioxide capturing surface layer coating according to claim 1, wherein the particle size of the calcium silicate particles is in the range of 0.1-0.5mm and the relative density is 2.5-3.0.\|5. The method for preparing the water-based carbon dioxide capture surface coating according to claim 1, wherein the rock wool fibers are common rock wool fibers.\|6. The method for preparing the water-based carbon dioxide capturing surface layer paint as claimed in claim 1, comprising:\| Mixing dilute cement paste with the water cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers according to a certain mass ratio, and uniformly stirring to obtain a directly-smeared coating; or (b) \|The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray-type functional coating is obtained.\|7. The method for preparing the water-based carbon dioxide capture surface coating according to claim 1, wherein the prepared surface coating can be directly smeared or sprayed on the outer surface of a structure, and the thickness of the coating is 0.2-0.5cm.	(CN116463001)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of carbon capture, in particular to a water-medium carbon dioxide capture surface layer coating and a preparation method thereof.\|BACKGROUND ART\|[0002] The capture and sequestration (CCS) of high concentration CO 2 emitted by point sources during the transition period may reduce the emissions of CO 2. However, the aim of stabilizing the CO 2 in the atmosphere below 450ppm is not possible with CCS alone. The concentration of carbon dioxide in air has increased from around 200ppm before the industrial revolution to over 400ppm at present, and therefore, the development of technology for directly capturing carbon dioxide from the surrounding air is also an effective means for slowing down climate change and is urgent.\|DISCLOSURE\|Disclosure of Invention\|[0003] The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried; when the air is wet, carbon dioxide in the gaps of the coating layer is converted into carbonate or bicarbonate to be released, and the carbonate or bicarbonate is flushed with water to enter the water body, so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled, and the problems in the background art are solved.\|[0004] In order to achieve the above purpose, the present invention provides the following technical solutions:\|[0005] A preparation method of water medium carbon dioxide capturing surface layer coating comprises polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion; wherein the mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%. \|[0006] Furthermore, the polystyrene quaternary ammonium salt resin is a main component for capturing carbon dioxide in a water medium, and can be prepared by adopting commercial powder particles or self-preparation, and the particle size is 0.2-1.0mm.\|[0007] Further, the preparation method of the polystyrene quaternary ammonium salt resin comprises the following steps:\|[0008] s1: completely immersing 10 parts of chloromethyl polystyrene resin powder in N, N-Dimethylformamide (DMF) according to the mass ratio, and swelling for 24 hours at 30-40 ℃; \|[0009] s2: adding 2 parts of polyethylenimine, and soaking for 12 hours at 30-40 ℃; \|[0010] s3: soaking in ethanol for 12 hours, filtering and drying; \|[0011] S4: swelling with isopropanol for 24 hours, adding 5 parts of 1 bromododecane for quaternization at 80-85 ℃ for 24 hours, and then adding 1.5 parts of 1 bromobutane for intensive quaternization at 45-50 ℃ for 4 hours; \|[0012] s5: and finally, filtering at room temperature, washing with ethanol and drying to obtain the quaternary ammonium salt modified polystyrene resin powder particles. \|[0013] Further, the hydrotalcite-like mineral is a layered double metal hydroxide composed of Ca/Al/Mg metal oxide, which is derived from natural hydrohead ore, and is assembled by non-covalent bond interaction between positively charged octahedral host laminates and interlayer anions, and has a particle size ranging from 0.1 to 1.0mm.\|[0014] Furthermore, the diatomite is in a powder shape, the particle size is 0.5-1.0mm, and the huge specific surface area of the diatomite particles is beneficial to the adsorption and exchange of gas.\|[0015] Furthermore, the particle size range of the calcium silicate particles is 0.1-0.5mm, and the relative density is 2.5-3.0, so that the calcium silicate has the functions of flame retardance, heat preservation, heat insulation, antibiosis and mildew prevention.\|[0016] Furthermore, the rock wool fiber is common rock wool fiber and is used for increasing the void ratio of the coating and facilitating gas exchange.\|[0017] Still further, the method includes:\|[0018] Mixing dilute cement paste with the water cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers according to a certain mass ratio, and uniformly stirring to obtain a directly-smeared coating; or (b) \|[0019] The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray coating type paint is obtained.\|[0020] Furthermore, the prepared surface layer coating can be directly and uniformly coated or sprayed on the outer surface of the structure, the thickness of the coating is 0.2-0.5cm, and the carbon respiration function of the outer surface of the structure can be realized, namely, carbon dioxide is absorbed when air is gradually dried, and carbon dioxide is released when the air is wet.\|[0021] Compared with the prior art, the invention has the beneficial effects that:\|[0022] The invention provides a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the water medium carbon dioxide capturing surface layer coating is mainly composed of polystyrene quaternary ammonium salt resin (mass portion 10-15), hydrotalcite-like minerals (mass portion 10-15), diatomite (mass portion 3-5), calcium silicate (mass portion 17-25), rock wool fibers (mass portion 3-5) and dilute cement paste (mass portion 35-57) according to a certain mass mixing proportion, the coating is smeared on the surface of a building, carbon dioxide can be automatically captured from air when a coating layer is dried, carbon dioxide can be desorbed by the coating layer and dissolved in water in a carbonate form to flow out when the coating layer is wet, the carbon dioxide in the air is automatically captured by taking water as a medium, and the carbon dioxide breathing function of the outer facade of the building can be realized. \|[0023] The conception, specific structure, and technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, features, and effects of the present invention.\|DRAWINGS DESCRIPTION\|[0024] The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate embodiments of the application and together with the description serve to explain the application.\|[0025] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for the description of the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0026] FIG. 1 is a schematic illustration of the carbon dioxide absorption and release process mechanism of the coating of the present invention;\|[0027] FIG. 2 is a schematic illustration of the application of the coating of the present invention to a facade of a structure; \|[0028] FIG. 3 is a schematic diagram of hydrotalcite-like minerals according to the present invention. \|INVENTION MODE\|Detailed Description\|[0029] Other advantages and effects of the present invention will become apparent to those skilled in the art from the following disclosure, which describes the embodiments of the present invention with reference to specific examples. The invention may be practiced or carried out in other embodiments that depart from the specific details, and the details of the present description may be modified or varied from the spirit and scope of the present invention. It should be noted that the following embodiments and features in the embodiments may be combined with each other without conflict.\|[0030] It should be noted that the illustrations provided in the following embodiments merely illustrate the basic concept of the present invention by way of illustration, and only the components related to the present invention are shown in the illustrations, not according to the number, shape and size of the components in actual implementation, and the form, number and proportion of each component in actual implementation may be arbitrarily changed, and the layout of the components may be more complex.\|[0031] Some exemplary embodiments of the invention have been described for illustrative purposes, it being understood that the invention may be practiced otherwise than as specifically shown in the accompanying drawings.\|[0032] The embodiment of the invention provides a preparation method of a water medium carbon dioxide capturing surface layer coating, which consists of polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion.\|[0033] The polystyrene quaternary ammonium salt resin is a main component for realizing carbon dioxide capture of a water medium, can be prepared from commercial powder particles with the particle size of 0.2-1.0mm, has the mass ratio of 10-15% in the coating, and has a certain mildew-proof and bactericidal effect and is beneficial to mildew prevention of the coating.\|[0034] The preparation method of the polystyrene quaternary ammonium salt resin comprises the following steps:\|[0035] s1: completely immersing 10 parts of chloromethyl polystyrene resin powder in N, N-Dimethylformamide (DMF) according to the mass ratio, and swelling for 24 hours at 30-40 ℃; \|[0036] s2: adding 2 parts of polyethylenimine, and soaking for 12 hours at 30-40 ℃; \|[0037] s3: soaking in ethanol for 12 hours, filtering and drying; \|[0038] S4: swelling with isopropanol for 24 hours, adding 5 parts of 1 bromododecane for quaternization at 80-85 ℃ for 24 hours, and then adding 1.5 parts of 1 bromobutane for intensive quaternization at 45-50 ℃ for 4 hours; \|[0039] s5: and finally, filtering at room temperature, washing with ethanol and drying to obtain the quaternary ammonium salt modified polystyrene resin powder particles. \|[0040] The synthetic process route of the polystyrene quaternary ammonium salt resin is as follows:\|[0041] \|[0042] In the embodiment of the invention, the hydrotalcite-like mineral is mainly a layered double metal hydroxide formed by Ca/Al/Mg metal oxide, is derived from natural hydrofluorite, is assembled by non-covalent bond interaction between a main body laminate of an octahedron (calcoxy, magnesia octahedron or alumina octahedron) with positive charges and an interlayer anion, and has a structure shown in figure 3 (wherein M represents Ca, al or Mg; A represents an anion). \|[0043] In order to reduce cost, natural hydrotalcite-like minerals can be directly adopted, the particle size range of the hydrotalcite-like minerals is 0.1-1.0mm, and the mass ratio of the hydrotalcite-like minerals in the paint is 10-15%.\|[0044] Specifically, hydrotalcite-like minerals can be purchased from the following web sites:\|[0045] aluminum magnesium hydrotalcite (Tianjin balance blue sea technology limited): \|[0046] https://detail.1688.com/offer/661622986146.htmlexp=enquiry%3AB&spm=a312h.2018_new_sem.dh_002.4.753e4b3dwFlIOj&cosite=baidujj&tracelog=p4p&_p_isad=1&clickid=d03616eec8864d809dce520d1839c01d&sessionid=cfdd5b610ea8464e0d77c3b1871a9264&a=1416&e=KWo.0gR-IlmQgV3XCjgNJ7LfaupOvlS.jc7eTz15fCH9PqbBDDQSDzB3m4XMOgA2e2OtVP1Jh4sb7AJCzkOHH5ZgSgUQMMbOH9p4ldzbdqEkTW.VtH..9uIaYQ4Zs.dt.o8k8junxwtz3zM49yD9eKsE2ZV6JcpvnCOJLKxPYQ96Hg0R6Cv1gtCPyb20.DQ8nuhLQNZ9dqHjqfl.RGtZYkVHyVZEqONRqtYzmCIrysY3GBxjBoOQaM5Jy6mnZopXvloJuMZHzzi885SgK3ZLXw__&sk=sem&style=1.\|[0047] aluminum magnesium hydrotalcite (Jin Shuiou Hongyuan chemical industry business, zheng state): \|[0048] https://detail.1688.com/offer/588588278288.html&idx=50。\|[0049] Aluminum-calcium hydrotalcite (Jining Sanshi biotechnology Co., ltd.): \|[0050] https://detail.1688.com/offer/677407307296.html&idx=55。\|[0051] The hydrotalcite-like mineral is helpful for the paint to realize the adsorption and release of carbonate anions and bicarbonate anions. Meanwhile, the hydrotalcite mineral has the capability of absorbing infrared light with specific wavelength, can accelerate the heating and drying of the paint, accelerates the absorption of carbon dioxide by the paint, and is more conducive to the realization of the absorption of infrared wave bands after the hydrotalcite-like mineral is combined with the organic ion exchange resin. \|[0052] The diatomite in the embodiment of the invention is in a powder shape, the particle size is 0.5-1.0mm, the mass fraction is 3-5%, and the huge specific surface area of the diatomite particles is beneficial to the adsorption and exchange of gas.\|[0053] The particle size range of the calcium silicate particles in the embodiment of the invention is 0.1-0.5mm, the relative density is 2.5-3.0, the mass ratio of the calcium silicate particles in the coating is 17-25%, and the calcium silicate can increase the functions of flame retardance, heat preservation, heat insulation, antibiosis and mildew resistance of the surface of a structure.\|[0054] The rock wool fiber in the embodiment of the invention is common basalt rock wool fiber, the mass share of the rock wool fiber is 3-5%, the fiber length is 1-5cm, and the rock wool fiber has the main function of increasing the void ratio of the coating and is beneficial to gas exchange.\|[0055] According to the application mode of the coating, the water-cement ratio of the dilute cement slurry is divided into two types, and the dilute cement slurry with the water-cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly stirred according to a certain mass ratio, so that the directly smeared coating is obtained; or alternatively\|[0056] The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray coating type paint is obtained.\|[0057] The carbon breath of the structure to carbon dioxide can be realized by painting the paint on the outer surface of the structure (the thickness of the coating is 0.2-0.5 cm), namely, carbon dioxide is absorbed when air is gradually dried, and carbon dioxide is released when the air is wet.\|[0058] The research and development principle of the invention: according to prior art documents, materials that successfully achieve direct capture of carbon dioxide from air generally require that 4 conditions be met:\|[0059] (1) Rapid reaction kinetics, and can rapidly absorb carbon dioxide; (2) the cost is low enough to facilitate the development and popularization of the application; (3) the application scene is wide, and large-scale application can be developed; (4) The method is convenient for rapid regeneration under general environmental conditions, and can complete the whole CO 2 capturing-releasing cycle. \|[0060] In practice, however, there are a number of substances that can achieve carbon dioxide adsorption, but it is difficult to achieve regeneration under normal environmental conditions (condition (4) is not satisfied), because they must overcome a large energy barrier to regenerate. For example, the heat of adsorption required for the calcium-based calcination process and the sodium-based decomposition hydrolysis process are 179kJ/mol CO 2 and 135kJ/mol CO 2, respectively, and the amine-based adsorbent has a heat of adsorption for CO 2 of about 80kJ/mol CO 2, respectively. They require a large amount of energy if they need to be released again after adsorbing carbon dioxide, which in turn leads to carbon dioxide emissions.\|[0061] Therefore, the embodiment of the invention provides the energy-saving adsorbent taking water as a medium, carbon dioxide can be captured and released only by means of the water medium in contact with the material, compared with other adsorption materials, the adsorption heat of the ion exchange resin is only 32kJ/mol CO 2, and when the relative humidity of air is increased from 15% to 100%, the equilibrium partial pressure of CO 2 on the polystyrene quaternary ammonium salt ion exchange resin is increased by 2 orders of magnitude, namely, the carbon dioxide adsorbed in the polystyrene quaternary ammonium salt ion exchange resin is obviously released due to the increase of the air humidity. This effect is due on the one hand to the physical competitive adsorption of water vapor and carbon dioxide by the polystyrene quaternary ammonium ion exchange resin and on the other hand to the good affinity of the polystyrene quaternary ammonium ion exchange resin for CO 2 when dried.\|[0062] The principle of the polystyrene quaternary ammonium salt ion exchange resin is as follows: with the air-drying process in-line with the air-drying process, The positively charged adsorbed CO 32- in the quaternary ammonium salt and water molecules in the material gaps are converted into HCO 3-, Thereby freeing up an adsorption site for the absorption of OH -, while OH - absorbs CO 2 from the air and converts it to HCO 3-, the process thus achieves direct capture of carbon dioxide in the air; when the air is wet, the air is in contact with the air, The 2 HCO 3- are combined and converted into CO 32- and CO 2 are carried away by water, Part of CO 32- occupies 2 positive charge adsorption sites in the quaternary ammonium salt. I.e., adsorption/desorption of CO 2, can be expressed as a series of reactions: dissociation of water, formation of bicarbonate, adsorption of CO 2 on hydroxide, release of carbonate from bicarbonate back and release of CO 2. The main chemical process is shown in the following formula and is shown in the attached figure 1.\|[0063] H2O=H++OH-\|[0064] CO32-+H+=HCO3-\|[0065] OH-+CO2=HCO3-\|[0066] HCO3-+HCO3-=CO32-+CO2+H2O\|[0067] In order to meet 4 conditions of successfully realizing direct capture of carbon dioxide materials from air, the embodiment of the invention provides a water medium carbon dioxide capture surface layer coating and a preparation method thereof. Mainly comprises polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion.\|[0068] For further better explanation of the invention, the following specific embodiments are provided:\|[0069] 10 g of polystyrene quaternary ammonium salt ion exchange resin balls (particle size of 0.5 mm), 10 g of hydrotalcite mineral particles (particle size of 0.5 mm), 3 g of diatomite particles (particle size of 0.5-1.0 mm), 17 g of calcium silicate (particle size of 0.5 mm), 3 g of rock wool fibers (basalt fibers for common insulation boards) and 57 g of dilute cement paste (water cement ratio of 0.75) are mixed, firstly, manual pre-mixing is carried out, then the mixture is put into a beaker, and mechanical mixing is carried out for 30min by using a dispersing machine, and the stirring speed is 18-22r/min. About 100 grams of coating was finally obtained. \|[0070] As shown in FIG. 2, a portion of the coating was spread on a 10cm by 10cm tile surface to a thickness of 0.5mm and then dried in a vacuum oven at 105℃for 24 hours to ensure complete drying of the coating, which removed carbon dioxide and moisture incorporated within the coating. The tile is then quickly placed in a sample cell (30 cm x 30cm closed plexiglass box) that is connected to an infrared gas analyzer LICOR840, and the carbon dioxide concentration and dew point (the greater the relative humidity, the higher the dew point temperature) of the sample cell can be obtained in real time.\|[0071] As can be seen by instrumental observation, the concentration of carbon dioxide in the sample chamber was reduced from 800ppm to 400ppm over 60min and to 320ppm over 120min after the dried tile coated with the coating was placed, indicating that the dried coating layer had the ability to absorb ("call in") carbon dioxide. After 120min, water vapor was slowly introduced to raise the dew point from 6deg.C to 16deg.C (relative humidity from about 30% to about 60%), and after 60min the carbon dioxide concentration level in the sample chamber gradually increased to 456ppm, indicating that the wet coating layer had the ability to release ("exhale") carbon dioxide. That is, the coating layer has a function of achieving carbon dioxide "breathing" by dry-wet alternation.\|[0072] To sum up: the invention provides a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the water medium carbon dioxide capturing surface layer coating is mainly composed of polystyrene quaternary ammonium salt resin (mass portion 10-15), hydrotalcite-like minerals (mass portion 10-15), diatomite (mass portion 3-5), calcium silicate (mass portion 17-25), rock wool fibers (mass portion 3-5) and dilute cement paste (mass portion 35-57) according to a certain mass mixing proportion, the coating is smeared on the surface of a building, carbon dioxide can be automatically captured from air when a coating layer is dried, carbon dioxide can be desorbed by the coating layer and dissolved in water in a carbonate form to flow out when the coating layer is wet, the carbon dioxide in the air is automatically captured by taking water as a medium, and the carbon dioxide breathing function of the outer facade of the building can be realized.\|[0073] The technical features of the above embodiments may be arbitrarily combined, and all possible combinations of the technical features in the above embodiments are not described for brevity of description, however, as long as there is no contradiction between the combinations of the technical features, they should be considered as the scope of the description.\|[0074] The above embodiments are merely illustrative of the principles of the present invention and its effectiveness, and are not intended to limit the invention. Modifications and variations may be made to the above-described embodiments by those skilled in the art without departing from the spirit and scope of the invention. Accordingly, it is intended that all equivalent modifications and variations of the invention be covered by the claims, which are within the ordinary skill of the art, be within the spirit and scope of the present disclosure.	(CN116463001)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of carbon capture, in particular to a water-medium carbon dioxide capture surface layer coating and a preparation method thereof.\|BACKGROUND ART\|[0002] The capture and sequestration (CCS) of high concentration CO 2 emitted by point sources during the transition period may reduce the emissions of CO 2. However, the aim of stabilizing the CO 2 in the atmosphere below 450ppm is not possible with CCS alone. The concentration of carbon dioxide in air has increased from around 200ppm before the industrial revolution to over 400ppm at present, and therefore, the development of technology for directly capturing carbon dioxide from the surrounding air is also an effective means for slowing down climate change and is urgent.\|DISCLOSURE\|Disclosure of Invention\|[0003] The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried; when the air is wet, carbon dioxide in the gaps of the coating layer is converted into carbonate or bicarbonate to be released, and the carbonate or bicarbonate is flushed with water to enter the water body, so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled, and the problems in the background art are solved.\|[0004] In order to achieve the above purpose, the present invention provides the following technical solutions:\|[0005] A preparation method of water medium carbon dioxide capturing surface layer coating comprises polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion; wherein the mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%. \|[0006] Furthermore, the polystyrene quaternary ammonium salt resin is a main component for capturing carbon dioxide in a water medium, and can be prepared by adopting commercial powder particles or self-preparation, and the particle size is 0.2-1.0mm.\|[0007] Further, the preparation method of the polystyrene quaternary ammonium salt resin comprises the following steps:\|[0008] s1: completely immersing 10 parts of chloromethyl polystyrene resin powder in N, N-Dimethylformamide (DMF) according to the mass ratio, and swelling for 24 hours at 30-40 ℃; \|[0009] s2: adding 2 parts of polyethylenimine, and soaking for 12 hours at 30-40 ℃; \|[0010] s3: soaking in ethanol for 12 hours, filtering and drying; \|[0011] S4: swelling with isopropanol for 24 hours, adding 5 parts of 1 bromododecane for quaternization at 80-85 ℃ for 24 hours, and then adding 1.5 parts of 1 bromobutane for intensive quaternization at 45-50 ℃ for 4 hours; \|[0012] s5: and finally, filtering at room temperature, washing with ethanol and drying to obtain the quaternary ammonium salt modified polystyrene resin powder particles. \|[0013] Further, the hydrotalcite-like mineral is a layered double metal hydroxide composed of Ca/Al/Mg metal oxide, which is derived from natural hydrohead ore, and is assembled by non-covalent bond interaction between positively charged octahedral host laminates and interlayer anions, and has a particle size ranging from 0.1 to 1.0mm.\|[0014] Furthermore, the diatomite is in a powder shape, the particle size is 0.5-1.0mm, and the huge specific surface area of the diatomite particles is beneficial to the adsorption and exchange of gas.\|[0015] Furthermore, the particle size range of the calcium silicate particles is 0.1-0.5mm, and the relative density is 2.5-3.0, so that the calcium silicate has the functions of flame retardance, heat preservation, heat insulation, antibiosis and mildew prevention.\|[0016] Furthermore, the rock wool fiber is common rock wool fiber and is used for increasing the void ratio of the coating and facilitating gas exchange.\|[0017] Still further, the method includes:\|[0018] Mixing dilute cement paste with the water cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers according to a certain mass ratio, and uniformly stirring to obtain a directly-smeared coating; or (b) \|[0019] The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray coating type paint is obtained.\|[0020] Furthermore, the prepared surface layer coating can be directly and uniformly coated or sprayed on the outer surface of the structure, the thickness of the coating is 0.2-0.5cm, and the carbon respiration function of the outer surface of the structure can be realized, namely, carbon dioxide is absorbed when air is gradually dried, and carbon dioxide is released when the air is wet.\|[0021] Compared with the prior art, the invention has the beneficial effects that:\|[0022] The invention provides a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the water medium carbon dioxide capturing surface layer coating is mainly composed of polystyrene quaternary ammonium salt resin (mass portion 10-15), hydrotalcite-like minerals (mass portion 10-15), diatomite (mass portion 3-5), calcium silicate (mass portion 17-25), rock wool fibers (mass portion 3-5) and dilute cement paste (mass portion 35-57) according to a certain mass mixing proportion, the coating is smeared on the surface of a building, carbon dioxide can be automatically captured from air when a coating layer is dried, carbon dioxide can be desorbed by the coating layer and dissolved in water in a carbonate form to flow out when the coating layer is wet, the carbon dioxide in the air is automatically captured by taking water as a medium, and the carbon dioxide breathing function of the outer facade of the building can be realized. \|[0023] The conception, specific structure, and technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, features, and effects of the present invention.\|DRAWINGS DESCRIPTION\|[0024] The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate embodiments of the application and together with the description serve to explain the application.\|[0025] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for the description of the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0026] FIG. 1 is a schematic illustration of the carbon dioxide absorption and release process mechanism of the coating of the present invention;\|[0027] FIG. 2 is a schematic illustration of the application of the coating of the present invention to a facade of a structure; \|[0028] FIG. 3 is a schematic diagram of hydrotalcite-like minerals according to the present invention. \|INVENTION MODE\|Detailed Description\|[0029] Other advantages and effects of the present invention will become apparent to those skilled in the art from the following disclosure, which describes the embodiments of the present invention with reference to specific examples. The invention may be practiced or carried out in other embodiments that depart from the specific details, and the details of the present description may be modified or varied from the spirit and scope of the present invention. It should be noted that the following embodiments and features in the embodiments may be combined with each other without conflict.\|[0030] It should be noted that the illustrations provided in the following embodiments merely illustrate the basic concept of the present invention by way of illustration, and only the components related to the present invention are shown in the illustrations, not according to the number, shape and size of the components in actual implementation, and the form, number and proportion of each component in actual implementation may be arbitrarily changed, and the layout of the components may be more complex.\|[0031] Some exemplary embodiments of the invention have been described for illustrative purposes, it being understood that the invention may be practiced otherwise than as specifically shown in the accompanying drawings.\|[0032] The embodiment of the invention provides a preparation method of a water medium carbon dioxide capturing surface layer coating, which consists of polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion.\|[0033] The polystyrene quaternary ammonium salt resin is a main component for realizing carbon dioxide capture of a water medium, can be prepared from commercial powder particles with the particle size of 0.2-1.0mm, has the mass ratio of 10-15% in the coating, and has a certain mildew-proof and bactericidal effect and is beneficial to mildew prevention of the coating.\|[0034] The preparation method of the polystyrene quaternary ammonium salt resin comprises the following steps:\|[0035] s1: completely immersing 10 parts of chloromethyl polystyrene resin powder in N, N-Dimethylformamide (DMF) according to the mass ratio, and swelling for 24 hours at 30-40 ℃; \|[0036] s2: adding 2 parts of polyethylenimine, and soaking for 12 hours at 30-40 ℃; \|[0037] s3: soaking in ethanol for 12 hours, filtering and drying; \|[0038] S4: swelling with isopropanol for 24 hours, adding 5 parts of 1 bromododecane for quaternization at 80-85 ℃ for 24 hours, and then adding 1.5 parts of 1 bromobutane for intensive quaternization at 45-50 ℃ for 4 hours; \|[0039] s5: and finally, filtering at room temperature, washing with ethanol and drying to obtain the quaternary ammonium salt modified polystyrene resin powder particles. \|[0040] The synthetic process route of the polystyrene quaternary ammonium salt resin is as follows:\|[0041] \|[0042] In the embodiment of the invention, the hydrotalcite-like mineral is mainly a layered double metal hydroxide formed by Ca/Al/Mg metal oxide, is derived from natural hydrofluorite, is assembled by non-covalent bond interaction between a main body laminate of an octahedron (calcoxy, magnesia octahedron or alumina octahedron) with positive charges and an interlayer anion, and has a structure shown in figure 3 (wherein M represents Ca, al or Mg; A represents an anion). \|[0043] In order to reduce cost, natural hydrotalcite-like minerals can be directly adopted, the particle size range of the hydrotalcite-like minerals is 0.1-1.0mm, and the mass ratio of the hydrotalcite-like minerals in the paint is 10-15%.\|[0044] Specifically, hydrotalcite-like minerals can be purchased from the following web sites:\|[0045] aluminum magnesium hydrotalcite (Tianjin balance blue sea technology limited): \|[0046] https://detail.1688.com/offer/661622986146.htmlexp=enquiry%3AB&spm=a312h.2018_new_sem.dh_002.4.753e4b3dwFlIOj&cosite=baidujj&tracelog=p4p&_p_isad=1&clickid=d03616eec8864d809dce520d1839c01d&sessionid=cfdd5b610ea8464e0d77c3b1871a9264&a=1416&e=KWo.0gR-IlmQgV3XCjgNJ7LfaupOvlS.jc7eTz15fCH9PqbBDDQSDzB3m4XMOgA2e2OtVP1Jh4sb7AJCzkOHH5ZgSgUQMMbOH9p4ldzbdqEkTW.VtH..9uIaYQ4Zs.dt.o8k8junxwtz3zM49yD9eKsE2ZV6JcpvnCOJLKxPYQ96Hg0R6Cv1gtCPyb20.DQ8nuhLQNZ9dqHjqfl.RGtZYkVHyVZEqONRqtYzmCIrysY3GBxjBoOQaM5Jy6mnZopXvloJuMZHzzi885SgK3ZLXw__&sk=sem&style=1.\|[0047] aluminum magnesium hydrotalcite (Jin Shuiou Hongyuan chemical industry business, zheng state): \|[0048] https://detail.1688.com/offer/588588278288.html&idx=50。\|[0049] Aluminum-calcium hydrotalcite (Jining Sanshi biotechnology Co., ltd.): \|[0050] https://detail.1688.com/offer/677407307296.html&idx=55。\|[0051] The hydrotalcite-like mineral is helpful for the paint to realize the adsorption and release of carbonate anions and bicarbonate anions. Meanwhile, the hydrotalcite mineral has the capability of absorbing infrared light with specific wavelength, can accelerate the heating and drying of the paint, accelerates the absorption of carbon dioxide by the paint, and is more conducive to the realization of the absorption of infrared wave bands after the hydrotalcite-like mineral is combined with the organic ion exchange resin. \|[0052] The diatomite in the embodiment of the invention is in a powder shape, the particle size is 0.5-1.0mm, the mass fraction is 3-5%, and the huge specific surface area of the diatomite particles is beneficial to the adsorption and exchange of gas.\|[0053] The particle size range of the calcium silicate particles in the embodiment of the invention is 0.1-0.5mm, the relative density is 2.5-3.0, the mass ratio of the calcium silicate particles in the coating is 17-25%, and the calcium silicate can increase the functions of flame retardance, heat preservation, heat insulation, antibiosis and mildew resistance of the surface of a structure.\|[0054] The rock wool fiber in the embodiment of the invention is common basalt rock wool fiber, the mass share of the rock wool fiber is 3-5%, the fiber length is 1-5cm, and the rock wool fiber has the main function of increasing the void ratio of the coating and is beneficial to gas exchange.\|[0055] According to the application mode of the coating, the water-cement ratio of the dilute cement slurry is divided into two types, and the dilute cement slurry with the water-cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly stirred according to a certain mass ratio, so that the directly smeared coating is obtained; or alternatively\|[0056] The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray coating type paint is obtained.\|[0057] The carbon breath of the structure to carbon dioxide can be realized by painting the paint on the outer surface of the structure (the thickness of the coating is 0.2-0.5 cm), namely, carbon dioxide is absorbed when air is gradually dried, and carbon dioxide is released when the air is wet.\|[0058] The research and development principle of the invention: according to prior art documents, materials that successfully achieve direct capture of carbon dioxide from air generally require that 4 conditions be met:\|[0059] (1) Rapid reaction kinetics, and can rapidly absorb carbon dioxide; (2) the cost is low enough to facilitate the development and popularization of the application; (3) the application scene is wide, and large-scale application can be developed; (4) The method is convenient for rapid regeneration under general environmental conditions, and can complete the whole CO 2 capturing-releasing cycle. \|[0060] In practice, however, there are a number of substances that can achieve carbon dioxide adsorption, but it is difficult to achieve regeneration under normal environmental conditions (condition (4) is not satisfied), because they must overcome a large energy barrier to regenerate. For example, the heat of adsorption required for the calcium-based calcination process and the sodium-based decomposition hydrolysis process are 179kJ/mol CO 2 and 135kJ/mol CO 2, respectively, and the amine-based adsorbent has a heat of adsorption for CO 2 of about 80kJ/mol CO 2, respectively. They require a large amount of energy if they need to be released again after adsorbing carbon dioxide, which in turn leads to carbon dioxide emissions.\|[0061] Therefore, the embodiment of the invention provides the energy-saving adsorbent taking water as a medium, carbon dioxide can be captured and released only by means of the water medium in contact with the material, compared with other adsorption materials, the adsorption heat of the ion exchange resin is only 32kJ/mol CO 2, and when the relative humidity of air is increased from 15% to 100%, the equilibrium partial pressure of CO 2 on the polystyrene quaternary ammonium salt ion exchange resin is increased by 2 orders of magnitude, namely, the carbon dioxide adsorbed in the polystyrene quaternary ammonium salt ion exchange resin is obviously released due to the increase of the air humidity. This effect is due on the one hand to the physical competitive adsorption of water vapor and carbon dioxide by the polystyrene quaternary ammonium ion exchange resin and on the other hand to the good affinity of the polystyrene quaternary ammonium ion exchange resin for CO 2 when dried.\|[0062] The principle of the polystyrene quaternary ammonium salt ion exchange resin is as follows: with the air-drying process in-line with the air-drying process, The positively charged adsorbed CO 32- in the quaternary ammonium salt and water molecules in the material gaps are converted into HCO 3-, Thereby freeing up an adsorption site for the absorption of OH -, while OH - absorbs CO 2 from the air and converts it to HCO 3-, the process thus achieves direct capture of carbon dioxide in the air; when the air is wet, the air is in contact with the air, The 2 HCO 3- are combined and converted into CO 32- and CO 2 are carried away by water, Part of CO 32- occupies 2 positive charge adsorption sites in the quaternary ammonium salt. I.e., adsorption/desorption of CO 2, can be expressed as a series of reactions: dissociation of water, formation of bicarbonate, adsorption of CO 2 on hydroxide, release of carbonate from bicarbonate back and release of CO 2. The main chemical process is shown in the following formula and is shown in the attached figure 1.\|[0063] H2O=H++OH-\|[0064] CO32-+H+=HCO3-\|[0065] OH-+CO2=HCO3-\|[0066] HCO3-+HCO3-=CO32-+CO2+H2O\|[0067] In order to meet 4 conditions of successfully realizing direct capture of carbon dioxide materials from air, the embodiment of the invention provides a water medium carbon dioxide capture surface layer coating and a preparation method thereof. Mainly comprises polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion.\|[0068] For further better explanation of the invention, the following specific embodiments are provided:\|[0069] 10 g of polystyrene quaternary ammonium salt ion exchange resin balls (particle size of 0.5 mm), 10 g of hydrotalcite mineral particles (particle size of 0.5 mm), 3 g of diatomite particles (particle size of 0.5-1.0 mm), 17 g of calcium silicate (particle size of 0.5 mm), 3 g of rock wool fibers (basalt fibers for common insulation boards) and 57 g of dilute cement paste (water cement ratio of 0.75) are mixed, firstly, manual pre-mixing is carried out, then the mixture is put into a beaker, and mechanical mixing is carried out for 30min by using a dispersing machine, and the stirring speed is 18-22r/min. About 100 grams of coating was finally obtained. \|[0070] As shown in FIG. 2, a portion of the coating was spread on a 10cm by 10cm tile surface to a thickness of 0.5mm and then dried in a vacuum oven at 105℃for 24 hours to ensure complete drying of the coating, which removed carbon dioxide and moisture incorporated within the coating. The tile is then quickly placed in a sample cell (30 cm x 30cm closed plexiglass box) that is connected to an infrared gas analyzer LICOR840, and the carbon dioxide concentration and dew point (the greater the relative humidity, the higher the dew point temperature) of the sample cell can be obtained in real time.\|[0071] As can be seen by instrumental observation, the concentration of carbon dioxide in the sample chamber was reduced from 800ppm to 400ppm over 60min and to 320ppm over 120min after the dried tile coated with the coating was placed, indicating that the dried coating layer had the ability to absorb ("call in") carbon dioxide. After 120min, water vapor was slowly introduced to raise the dew point from 6deg.C to 16deg.C (relative humidity from about 30% to about 60%), and after 60min the carbon dioxide concentration level in the sample chamber gradually increased to 456ppm, indicating that the wet coating layer had the ability to release ("exhale") carbon dioxide. That is, the coating layer has a function of achieving carbon dioxide "breathing" by dry-wet alternation.\|[0072] To sum up: the invention provides a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the water medium carbon dioxide capturing surface layer coating is mainly composed of polystyrene quaternary ammonium salt resin (mass portion 10-15), hydrotalcite-like minerals (mass portion 10-15), diatomite (mass portion 3-5), calcium silicate (mass portion 17-25), rock wool fibers (mass portion 3-5) and dilute cement paste (mass portion 35-57) according to a certain mass mixing proportion, the coating is smeared on the surface of a building, carbon dioxide can be automatically captured from air when a coating layer is dried, carbon dioxide can be desorbed by the coating layer and dissolved in water in a carbonate form to flow out when the coating layer is wet, the carbon dioxide in the air is automatically captured by taking water as a medium, and the carbon dioxide breathing function of the outer facade of the building can be realized.\|[0073] The technical features of the above embodiments may be arbitrarily combined, and all possible combinations of the technical features in the above embodiments are not described for brevity of description, however, as long as there is no contradiction between the combinations of the technical features, they should be considered as the scope of the description.\|[0074] The above embodiments are merely illustrative of the principles of the present invention and its effectiveness, and are not intended to limit the invention. Modifications and variations may be made to the above-described embodiments by those skilled in the art without departing from the spirit and scope of the invention. Accordingly, it is intended that all equivalent modifications and variations of the invention be covered by the claims, which are within the ordinary skill of the art, be within the spirit and scope of the present disclosure.	Family Number\|(100341084)\|100341084\|Object of Invention\|(CN114574045 A)\|The invention aims to provide a preparation method of a water - borne carbon dioxide capturing surface layer coating , which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried ; when the air is wet , carbon dioxide in the gaps of the coating ( . . . ) carbonate or bicarbonate to be released and then enters the water body along with water washing , so that the purpose of directly capturing carbon dioxide from the air and transferring the carbon dioxide to the water body is achieved , and the problems in the background art are solved . \|The invention discloses a preparation method of a water - borne carbon dioxide capturing surface layer coating , which is formed by mixing polystyrene quaternary ammonium salt resin ( 10-15 mass portions ) , hydrotalcite - like ( . . . ) the coating can desorb the carbon dioxide and is dissolved in water to flow out , water is used as a medium , the automatic capture of the carbon dioxide in the air is realized , and the carbon breathing function of the outer vertical surface of the building can be realized . The invention relates to the technical field of carbon capture , in particular to a preparation method of a surface coating for capturing carbon dioxide in a water medium . \|the invention provides a preparation method of a water - borne carbon dioxide capture surface layer coating , which is mainly composed of polystyrene quaternary ammonium salt resin ( mass portion 10-15 ) , hydrotalcite - like ( . . . ) the carbon dioxide in the form of carbonate in water to flow out , the device takes water as a medium , realizes automatic capture of carbon dioxide in the air , and can realize the carbon breathing function of the outer facade of the structure . \|(CN116463001 A)\|The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof , which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried ; when the air is wet , carbon dioxide in the gaps of the coating ( . . . ) be released , and the carbonate or bicarbonate is flushed with water to enter the water body , so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled , and the problems in the background art are solved . \|The invention discloses a water medium carbon dioxide capturing surface layer coating and a preparation method thereof , wherein the coating is composed of polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; the mass ratio of the polystyrene quaternary ammonium salt resin in the paint is 10-15% ; the mass ratio of hydrotalcite - like minerals in the paint is 10-15% ; ( . . . ) \|The invention relates to the technical field of carbon capture , in particular to a water - medium carbon dioxide capture surface layer coating and a preparation method thereof . \|(CN116463001B B)\|The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof , which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried ; when the air is wet , carbon dioxide in the gaps of the coating ( . . . ) be released , and the carbonate or bicarbonate is flushed with water to enter the water body , so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled , and the problems in the background art are solved . \|The invention discloses a water medium carbon dioxide capturing surface layer coating and a preparation method thereof , wherein the coating is composed of polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; the mass ratio of the polystyrene quaternary ammonium salt resin in the paint is 10-15% ; the mass ratio of hydrotalcite - like minerals in the paint is 10-15% ; ( . . . ) \|The invention relates to the technical field of carbon capture , in particular to a water - medium carbon dioxide capture surface layer coating and a preparation method thereof . \|Abstract\|(CN114574045 A)\|The invention discloses a preparation method of a water medium carbon dioxide capture surface coating . The coating is formed by mixing 10-15 parts by mass of polystyrene quaternary ammonium salt resin , 10-15 parts by mass of hydrotalcite - like minerals , 3-5 parts by mass of diatomite , 17-25 parts by mass of calcium silicate , 3-5 parts by mass of rock wool fibers and 35-57 parts by mass of thin cement paste according to a certain mass ratio , the coating is smeared on the surface of a building , and when a coating layer is dried , the coating layer is coated on the surface of the building . When the coating layer is wet , the coating layer can desorb the carbon dioxide and dissolve the carbon dioxide in water in a carbonate form to flow out , water serves as a medium , automatic capture of the carbon dioxide in the air is achieved , and the carbon breathing function of the outer vertical face of a building can be achieved . \|(CN116463001B B)\|The invention discloses a water medium carbon dioxide capture surface coating and a preparation method thereof . The water medium carbon dioxide capture surface coating is formed by mixing polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , kieselguhr , calcium silicate , rock wool fibers and thin cement paste according to a certain mass ratio . The mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15% ; the mass ratio of the hydrotalcite - like mineral in the coating is 10-15% ; the mass ratio of the diatomite in the coating is 3-5% ; the mass ratio of the calcium silicate in the coating is 17-25% ; the mass ratio of the rock wool fibers in the coating is 3-5% ; and the mass ratio of the thin cement paste in the coating is 35-57%. The coating is smeared on the surface of a building , and when a coating layer is dry , carbon dioxide can be automatically captured from air ; when the coating layer is wet , the coating layer can desorb carbon dioxide and dissolve the carbon dioxide in water in a carbonate form to flow out , so that the carbon breathing function of the external facade of the building is realized . \|Title\|(CN114574045 A)\|Preparation method of water medium carbon dioxide capture surface coating \|(CN116463001 A)\|Water medium carbon dioxide capture surface coating and preparation method thereof \|(CN116463001B B)\|Water medium carbon dioxide capturing surface layer coating and preparation method thereof \|Independent Claims\|(CN114574045 A)\|1. The preparation method of the water - borne carbon dioxide capturing surface coating is characterized by comprising polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement paste according to a certain mass mixing ratio . \|(CN116463001 A)\|1. The preparation method of the water medium carbon dioxide capturing surface layer coating is characterized by comprising polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; \|10. The water medium carbon dioxide capturing surface layer coating is characterized by being composed of polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; \|(CN116463001B B)\|1. The preparation method of the water medium carbon dioxide capturing surface layer coating is characterized by comprising polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; ( . . . ) \|	Basic materials chemistry	C09D-001/08\|C09D-007/61\|C09D-007/65\|C09D-007/70\|Y02C-020/40		C09D-001/08\|C09D-007/61\|C09D-007/65\|C09D-007/70\|Y02C-020/40	C09D-001/08\|C09D-007/61\|C09D-007/65\|C09D-125/06	C09D-001/08\|C09D-007/61\|C09D-007/65\|C09D-125/06			CN116463001B	CN116463001B 100341084 WHO=Examiner SELF=Y	CN113680334\|CN109575659\|CN108622951\|CN108043368\|CN107699089\|CN104056599\|CN103540199\|CN103958027\|KR20120028044\|CN114574045\|US20160229760	CN113680334 97148868 WHO=Examiner SELF=N CAT=A\|CN109575659 84062764 WHO=Examiner SELF=N CAT=A\|CN108622951 81572593 WHO=Examiner SELF=Y CAT=A\|CN108043368 79763962 WHO=Examiner SELF=N CAT=A\|CN107699089 78837473 WHO=Examiner SELF=N CAT=A\|CN104056599 67501607 WHO=Examiner SELF=N CAT=A\|CN103540199 59588170 WHO=Examiner SELF=N CAT=A\|CN103958027 94752751 WHO=Examiner SELF=N CAT=A\|KR20120028044 35317232 WHO=Examiner SELF=N CAT=A\|CN114574045 100341084 WHO=Examiner SELF=Y\|US20160229760 73830880 WHO=Examiner SELF=N	侯成龙: "季铵修饰聚合物的制备及空气二氧化碳捕集性能研究", 中国优秀博士学位论文全文数据库工程科技1辑, no. 1, pages 014 - 214 (Cat. Y)\|程磊: "氯甲基聚苯乙烯树脂接枝聚季铵盐型杀菌剂的制备及其杀菌性能", 石油化工, vol. 39, no. 1, pages 75 - 80 (Cat. Y)\|季铵修饰聚合物的制备及空气二氧化碳捕集性能研究;侯成龙;中国优秀博士学位论文全文数据库工程科技1辑(第第1期期);第B014-214页 (Cat. Y)\|氯甲基聚苯乙烯树脂接枝聚季铵盐型杀菌剂的制备及其杀菌性能;程磊;石油化工;第第39卷卷(第第1期期);第75-80页 (Cat. Y)\|滕巧巧: "“聚苯乙烯接枝聚乙烯亚胺树脂合成及Cu2+吸附”", 《化工进展》 (Cat. A)\|程磊等: "“氯甲基聚苯乙烯树脂接枝聚季铵盐型杀菌剂的制备及其杀菌性能”", 《石油化工》 (Cat. A)	KR20120028044; CN103958027; CN114574045; US20160229760\|CN103540199; CN104056599; CN107699089; CN108043368; CN108622951; CN109575659; CN113680334		GRANTED	(CN116463001)\|GRANTED\|(CN114574045)\|LAPSED	ALIVE	(CN116463001)\|ALIVE\|(CN114574045)\|DEAD	(CN116463001)\|LEGAL DETAILS FOR CN116463001\|Actual or expected expiration date=2043-03-15\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2023-03-15\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202310250007\|Application date=2023-03-15\|Standardized application number=2023CN-0250007\|Event publication date=2023-07-21\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN116463001\|Publication stage code=A\|Publication date=2023-07-21\|Standardized publication number=CN116463001\|Event publication date=2023-07-21\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2023-08-15\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2024-07-05\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN116463001\|Publication stage code=B\|Publication date=2024-07-05\|Standardized publication number=CN116463001B\|Event publication date=2024-07-05\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|(CN114574045)\|LEGAL DETAILS FOR CN114574045\|Actual or expected expiration date=2023-08-29\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-03-18\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202210271537\|Application date=2022-03-18\|Standardized application number=2022CN-0271537\|Event publication date=2022-06-03\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN114574045\|Publication stage code=A\|Publication date=2022-06-03\|Standardized publication number=CN114574045\|Event publication date=2022-06-03\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2022-06-21\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2023-08-29\|Event code=CN/WD01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent application deemed withdrawn after publication		(CN116463001)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQB4wlV1sYkERj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000073463133&ekey=2216&xpn=CN116463001B&kind=B	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=%252FUHDmbKj7zr%252Br9sAuSz3o7msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN116463001)\|CN\|(CN116463001)\|CN\|(CN114574045)\|CN	(CN116463001)\|NAME=SHANGHAI ZEYAO ENV PROT TECH CO LTD , COUNTRY=CN\|(CN116463001)\|NAME=SHANGHAI ZEYAO ENV PROT TECH CO LTD , COUNTRY=CN\|(CN114574045)\|NAME=SHANGHAI ZEYAO ENV PROT TECH CO LTD , COUNTRY=CN		(CN116463001)\|NAME=XU HAOJUN;SHANGHAI JIANQIU INTELLECTUAL PROPERTY ATTORNEYS , REG=31382\|(CN116463001)\|NAME=XU HAOJUN;SHANGHAI JIANQIU INTELLECTUAL PROPERTY ATTORNEYS , REG=31382\|(CN114574045)\|NAME=HE XINXIN;Hefei Du Lei Intellectual Property Agency (General Partnership) , REG=34227		(CN116463001)\|NAME=Song Xinshan\|NAME=Xu Yong\|NAME=Zhang Zhilan\|NAME=Wang Yuhui\|NAME=Xu Zhongshuo\|NAME=Wang Yifei\|NAME=Liu Yingying\|NAME=Tan Shujuan\|NAME=Huang Na\|NAME=Tang Haiyan\|(CN116463001)\|NAME=SONG XINSHAN\|NAME=XU YONG\|NAME=ZHANG ZHILAN\|NAME=WANG YUHUI\|NAME=XU ZHONGSHUO\|NAME=WANG YIFEI\|NAME=LIU YINGYING\|NAME=TAN SHUJUAN\|NAME=HUANG NA\|NAME=TANG HAIYAN\|(CN114574045)\|NAME=SONG XINSHAN\|NAME=XU YONG\|NAME=ZHANG ZHILAN\|NAME=WANG YUHUI\|NAME=XU ZHONGSHUO\|NAME=WANG YIFEI\|NAME=LIU YINGYING\|NAME=TAN SHUJUAN\|NAME=HUANG NA\|NAME=TANG HAIYAN	(CN116463001)\|3\|(CN114574045)\|2	1	2					(CN116463001)\|Number of Claims: NCL=7\|Gazette date: GAZDATE=2024-07-05\|Gazette number: GAZNUM=40-2702\|Number of Pages: NPAGES=10\|Primary examiner: 赵欢\|Primary examiner: Zhao Huan\|\|(CN116463001)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2023-07-21\|Gazette number: GAZNUM=39-2902\|Number of Pages: NPAGES=11\|Primary examiner: 赵欢\|Primary examiner: Zhao Huan\|\|(CN114574045)\|Number of Claims: NCL=9\|Gazette date: GAZDATE=2022-06-03\|Gazette number: GAZNUM=38-2202\|Number of Pages: NPAGES=9\|	(CN116463001)\|Previous publication: CN116463001 A 2023-07-21 [CN116463001]	(CN116463001)\|CHINESE (CHI)	(CN116463001B)\|Patent\|(CN116463001)\|Patent\|(CN114574045)\|Patent	Titre: (CN116463001)\|Water medium carbon dioxide capturing surface layer coating and preparation method thereof Résumé: (CN116463001)\|The invention discloses a water medium carbon dioxide capture surface coating and a preparation method thereof. The water medium carbon dioxide capture surface coating is formed by mixing polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, kieselguhr, calcium silicate, rock wool fibers and thin cement paste according to a certain mass ratio. The mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the coating is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; and the mass ratio of the thin cement paste in the coating is 35-57%. The coating is smeared on the surface of a building, and when a coating layer is dry, carbon dioxide can be automatically captured from air; when the coating layer is wet, the coating layer can desorb carbon dioxide and dissolve the carbon dioxide in water in a carbonate form to flow out, so that the carbon breathing function of the external facade of the building is realized.	9	Abstract	gpt-4o-mini	no	The article focuses on a surface coating for capturing CO₂ from the air, which does not involve the accelerated weathering of minerals or the specific processes related to mineral carbonation for carbon sequestration.
12	IN202441017388	IN202441017388	IN202441017388	116031041	IN202441017388 A 2025-09-12 [IN202441017388]	2024-03-11	2024-03-11	2025-09-12		(IN202441017388)\|2044-03-11	(IN202441017388)\|System and method for preparing carbonate-enhanced nutrition composition using geo-bags	(IN202441017388)\|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112. The system includes a rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The reactor 108 mixes crushed rocks and organic acid components to prepare a carbon-sequestration substrate. The geo-bag 112 is filled with the carbon-sequestration substrate, and the geo-bag 112 is made from eco-friendly materials, allowing selective exchange of components between the bag contents and the environment. The substrate in the geo-bag 112 is allowed to capture the CO2 from the atmosphereand convert the carbon-sequestration substrate into a carbonateenhanced nutrition composition, thereby reducing the environmental CO2 level. The composition includes high economic value materials like calcium carbonate, potash, phosphate, and heavy metals. The composition can be used as a fertilizer or building construction material like M-sand.	HYPERWORKS IMAGING PRIVATE	(IN202441017388)\|HYPERWORKS IMAGING PRIVATE LIMITED	Tannirkulam Ajay\|Margankunte Naveen	(IN202441017388)\|Tannirkulam Ajay\|Margankunte Naveen			(IN202441017388)\|1. A method for preparing a carbonate-enhanced nutrition composition using a geo-bag (112) wherein the method comprising: i) Collecting and crushing rocks into small particles, using a rock crushing unit (102); ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbon-sequestration substrate, using a reactor (108) by Characterized in that, a) mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions; and b) filling the carbon-sequestration substrate into the geo-bag (112) to prepare carbon-sequestration packages, wherein the geo-bag (112) comprises an ecofriendly material that permits only water and air to pass through while retaining the substrate inside, wherein the geo-bag (112) comprises a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbonsequestration substrate by subjecting the carbon-sequestration packages to a rockcarbonation period at an operating location to capture atmospheric carbon dioxide; wherein the geo-bag (112) acts as a structural member providing a high surface area-tovolume ratio to optimize carbon dioxide capture resulting 15 to 130 times enhanced carbonation efficiency.\|	(IN202441017388)\|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112.\|Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.\|	(IN202441017388)\|GEOBAG(100,42)\|CARBONATE ENHANCED NUTRITION(100,29)\|ROCK CRUSHING(57,8)\|CARBONSEQUESTRATION SUBSTRATE(48,2)\|CARBON SEQUESTRATION SUBSTRATE(44,31)\|ENHANCED CARBONATION(44,3)\|URBAN ORGANIC WASTAGE COLLECTION(41,4)\|CARBON SEQUESTRATION(37,42)\|ROCK CARBONATION PERIOD(35,9)\|MIX CRUSHED ROCK(33,1)\|CARBON DIOXIDE CAPTURE(32,1)\|GRAVEL(31,21)\|BIOMASS(28,12)\|CARBON SEQUESTRATION PACKAGE(26,8)\|SUBSTRATE INSIDE(26,1)\|MIXING CONDITION(24,6)\|FERTILIZER(24,4)\|ATMOSPHERIC CARBON DIOXIDE(24,2)\|ECOFRIENDLY MATERIAL(24,1)\|REACTOR(23,14)\|OUTDOOR ENVIRONMENT(23,4)\|BAG CONTENT(20,3)\|ORGANIC ACID EXTRACTION(19,8)\|ACETIC ACID COMPOUND(18,2)\|POTASH(17,6)\|GEOTEXTILE(17,4)\|MOISTURE CONTENT(17,4)\|AGRICULTURE(16,2)\|CARBON DIOXIDE(15,17)\|CALCIUM CARBONATE(15,6)\|DECOMPOSITION(15,3)\|MICROALGAE(15,3)\|CO2 LEVEL(15,2)\|OLIVINE(14,3)\|VOLUME RATIO(14,2)\|ACETIC ACID(13,8)\|ROCK CRUSHER(13,3)\|STONE WEIGHT(11,4)\|PH VALUE RANGING(11,3)\|ACCELERATE WEATHERING(11,2)\|CELLULOSE DERIVED MONOSACCHARIDE(11,2)\|CONCENTRATION LEVEL RANGING(11,2)\|HDPE(11,2)\|MAGNESIUM CARBONATE(11,2)\|SMALL PARTICLE(10,6)\|TRANSPORTATION MEDIUM(10,5)\|ECO FRIENDLY MATERIAL(10,4)\|BUILDING CONSTRUCTION(10,1)\|CARBONATED ENHANCED NUTRITION(10,1)\|THANTHE NATURAL CARBONATION(10,1)\|TOA CARBON MINERALIZATION(10,1)\|MIXING TEMPERATURE(9,4)\|SUPERCRITICAL CONDITION(9,4)\|DUNITE ANALYSIS(9,3)\|ELECTRO MICROBIAL PRODUCTION(9,2)\|REFILL CARTRIDGE(9,2)\|ROCK CARBONATION PERIOD RANGE(9,2)\|BASALT IC ROCK(9,1)\|LIQUEFIED BIOMASS CONVERSION(9,1)\|ORGANIC ACID COMPONENT(8,18)\|CONDITION OPTIMIZATION(8,6)\|EXPERIMENTAL SETUP(8,2)\|LIQUEFACTION REACTION(8,2)\|ACCELERATE CARBONATION(8,1)\|BIOMASS LIQUEFACTION(8,1)\|CONE CRUSHING(8,1)\|MINERAL DISSOLUTION REACTOR(8,1)\|STONE SIZE(7,12)\|CARBONIZATION(7,11)\|HEAVY METAL(7,6)\|CARBONATION MENSTRUATION(7,3)\|FURFURAL ACID LACTIC(7,3)\|STRUCTURAL MEMBER(7,3)\|VALUED MATERIAL(6,8)\|PPM(6,4)\|DIKETO GLUCONIC ACID(6,2)\|NONOPTIMIZED CONDITION(6,2)\|SAND SPRAY(6,2)\|BURIED FORA(6,1)\|CARBONATION REACTOR(6,1)\|CRUSHED ROCK RETRIEVAL(6,1)\|FARMING LAND(6,1)\|FEEDER BREAKER(6,1)\|MITIGATE ISSUE(6,1)\|NUTRITION ENHANCEMENT(6,1)\|RAW BASALT SAMPLE(6,1)\|RAW DUNITE SAMPLE(6,1)\|ATMOSPHERIC PRESSURE(5,4)\|CONSTRUCTION SITE(5,3)\|TRAPPING(5,3)\|BALL MILL CRUSHER(5,1)\|BASALT ANALYSIS(5,1)\|CARBONATION PERFORMANCE(5,1)\|DIKETOGLUCONIC ACID(5,1)\|DUNITEROCK SAMPLE(5,1)\|FEEDING ROCK(5,1)\|OPTIMIZED CARBONATION CONDITION(5,1)\|URBAN ORGANIC WASTE COLLECTION(5,1)\|FILLING STATION(4,4)\|GRAPHICAL REPRESENTATION(4,4)\|WEIGHT VOLUME(4,4)\|FIBER DENSITY(4,2)\|SOLID MINERAL(4,2)\|SYSTEM COMPLICATION(4,2)\|ASTHE REACTED CARBON REMAINS(4,1)\|BIO CATALYST COMBINATION(4,1)\|CARBON DIOXIDE SEQUESTRATION(4,1)\|CARBONATE ENHANCED MINERAL FORMATION(4,1)\|CARBONSEQUESTRATION(4,1)\|CO MINERALIZATION(4,1)\|DISPENSATION(4,1)\|EXCAVATOR(4,1)\|GYRATORY CRUSHER(4,1)\|OPTIMIZED ENVIRONMENT(4,1)\|PRIMARY COMPARTMENT(4,1)\|SIGNIFICANTRISEINATMOSPHERIC CARBON DIOXIDE(4,1)\|SYSTEMFORPREPARING(4,1)\|	(IN202441017388)\|1. A method for preparing a carbonate-enhanced nutrition composition using a geo-bag (112) wherein the method comprising: i) Collecting and crushing rocks into small particles, using a rock crushing unit (102); ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbon-sequestration substrate, using a reactor (108) by Characterized in that, a) mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions; and b) filling the carbon-sequestration substrate into the geo-bag (112) to prepare carbon-sequestration packages, wherein the geo-bag (112) comprises an ecofriendly material that permits only water and air to pass through while retaining the substrate inside, wherein the geo-bag (112) comprises a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbonsequestration substrate by subjecting the carbon-sequestration packages to a rockcarbonation period at an operating location to capture atmospheric carbon dioxide; wherein the geo-bag (112) acts as a structural member providing a high surface area-tovolume ratio to optimize carbon dioxide capture resulting 15 to 130 times enhanced carbonation efficiency.\|2. The method as claimed in claim 1, wherein the crushed rocks comprise at least one of olivine, dunite, ultramafic, basalt, serpentine, and/or a combination thereof, wherein the crushed rocks comprises of a particle size below 5 mm.\|3. The method as claimed in claim 1, wherein the predefined mixing conditions comprise a mixing temperature ranging from 25°C to 30°C and an atmospheric pressure ranging from 1 atm to 2 atm.\|4. The method as claimed in claim 1, wherein the carbon-sequestration substrate comprises a concentration level ranging from 400 part per million (ppm) to 450 ppm, a moisture content ranging from 25% to 95% of rock weight and has a pH value ranging from 2.5 to 3.5.\|5. The method as claimed in claim 1, wherein the geo-bag (112) comprises at least one of geotextiles, high-density polyethylene (HDPE), and/or a combination thereof.\|6. The method as claimed in claim 1, wherein the rock-carbonation period ranges from 2 years to 5 years.\|7. The method as claimed in claim 1, wherein the organic acid component is extracted using an electro-microbial production (EMP) technique from the biomass; wherein the biomass is generated from the decomposition of at least one of organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof.\|8. The method as claimed in claim 1, wherein the operating location comprises at least one of farming land, a construction site, an outdoor environment.\|9. The method as claimed in claim 1, wherein the method comprises extracting high-value materials from the carbonate-enhanced composition, wherein the high-value materials comprise at least one of magnesium carbonate, calcium carbonate, potash, phosphate, heavy metals and/or a combination thereof.\|10. The method as claimed in claim 1, wherein the carbonate-enhanced composition is used as fertilizer in agriculture and/or as M-sand in the construction field.	(IN202441017388)\|Technical Field\|[0001] The embodiments herein generally relate toa carbon mineralization method, and more particularly, a system and method for preparing carbonate-enhanced nutrition composition using a geo-bag. Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.\|Description of the Related Art\|[0002] In recent years, the significantriseinatmospheric carbon dioxide (CO2) levels has been identified as a leading cause of climate change on Earth. To mitigate this issue, carbon mineralization, or carbon sequestration, has emerged as a prominent method. Carbon mineralization is a process of converting carbon dioxide into solid minerals, such as carbonate, through a chemical reaction. This reaction occurs when specific types of rocks, such as serpentine, basalt, mafic, ultramafic, etc., are exposed to carbon dioxide, resulting in the formation of carbonate-enhanced minerals. Hence, the atmospheric CO2 level is stabilized asthe reacted carbon remains bound within the solid minerals, preventing its release into the atmosphere. However, it is important to note that this process typically requires several years to effectively reduce carbon levels in the atmosphere.\|[0003] Most of the existing carbon sequestration systemsto produce carbonate-enhanced mineralsutilize indoor techniques, employingan indirect method. For example, thesesystemsincludea mineral dissolution reactor for mixing various materials. These materials include magnesium or calcium, which is available in the rocks (e.g. serpentine, olivine, basalt, or labradorite), organic acid, and chelating agents. Through this mixing process, a magnesium or calcium-rich solvent is synthesized tocapture and store carbon dioxide. Additionally, these existing systemsinclude a combined biocatalyst and carbonation reactor, along witha control module for expediting the process of sequestration of carbon. However, the current indoor technique requires a more complicated arrangement and entails higher costs.\|[0004] Accordingly, there remains a need for a more simple and direct approach to capture and store the carbon dioxide from the atmosphere at a reduced economic level and to produce a carbonated enhanced nutrition composition using a geo-bag.\|SUMMARY\|[0005] In view of a foregoing, an embodiment herein provides a method for preparing a carbonate-enhanced nutrition composition using a geo-bag. The method includes i) collecting and crushing rocks into small particles, using a rock crushing unit; ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbonsequestration substrate using a reactor by mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions. The carbon-sequestration substrate is filled into geo-bags to prepare carbon-sequestration packages. The geo-bag includes an eco-friendly material that only permits water and air to pass through while retaining the substrate. The geo-bag consists of a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbon-sequestration substrate by subjecting the carbonsequestration packages to a rock-carbonation period at an operating location to capture atmospheric carbon dioxide. The geo-bag acts as a structural member providing a high surface area-to-volume ratio to optimize carbon dioxide capture resulting in 15 to 130 times enhanced carbonation efficiency.\|[0006] In some embodiments, the crushed rocks include at least one of olivine, dunite, ultramafic, basalt, serpentine, and/or a combination thereof. The crushed rocks include a particle size below 5 mm.\|[0007] In some embodiments, the predefined mixing conditions include a mixing temperature ranging from 25°C to 30°C and an atmospheric pressure ranging from 1 atm to 2\|atm.\|[0008] In some embodiments, the carbon-sequestration substrate includes a concentration level ranging from 400 parts per million (ppm) to 450 ppm, a moisture content ranging from\|25% to 95% of rock weight and a pH value ranging from 2.5 to 3.5.\|[0009] In some embodiments, the geo-bag includes at least one of the geotextiles, highdensity polyethylene (HDPE), and/or a combination thereof.\|[0010] In some embodiments, the rock-carbonation period ranges from 2 years to 5 years.\|[0011] In some embodiments, the organic acid component is extracted using an electromicrobial production (EMP) technique from the biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof.\|[0012] In some embodiments, the operating location includes at least one farming land, a construction site, and an outdoor environment.\|[0013] In some embodiments, the method includes extracting high-value materials from the carbonate-enhanced nutrition composition, wherein the high-value materials include at least one of magnesium carbonate, calcium carbonate, potash, phosphate, heavy metals, and/or a combination thereof.\|[0014] In some embodiments, the carbonate-enhanced nutrition composition is used as fertilizer in agriculture and/or as M-sand in the construction field.\|[0015] . In some embodiments, the refill docking platform includes a connection part that is configured to hold the refill cartridge in an invertedly upright position to enable the flow of the substance from the refill cartridge to the bottom of the primary compartment.\|[0016] The method of preparing a carbonate-enhanced nutrition composition of the present description includes a more direct approach for capturing and storing carbon dioxide from the atmosphere using the geo-bag. The direct approach represents the geo-bag that includes a simple configuration used in an outdoor environment for capturing and storing carbon dioxide from the atmosphere. Such a simple configuration of geo-bag eliminates the need for a complicated arrangement of the carbon dioxide sequestration system used in the existing system.\|The geo-bag includes improved measurement, reporting, and verification (MRV) by enclosing the first mixture in a high surface area to volume ratio and staking in vertical layers to hold the first mixture, and the geo-bag acts as a structural member to produce a carbonate enhanced nutrition composition at a lower economical level. Such carbonate-enhanced nutrition composition includes high economic value materials, which can be used as a fertilizer for agricultural fields or building construction material, e.g. M-sand.\|[0017] These and other aspects of the embodiments herein will be better appreciated and understood when considered in conjunction with the following description and the accompanying drawings. It should be understood, however, that the following descriptions, while indicating preferred embodiments and numerous specific details thereof, are given by way of illustration and not of limitation. Many changes and modifications may be made within the scope of the embodiments herein without departing from the spirit thereof, and the embodiments herein include all such modifications.\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] The embodiments herein will be better understood from the following detailed description with reference to the drawings, in which:\|[0019] FIG. 1 is a block diagram that illustrates a systemforpreparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein;\|[0020] FIG. 2 illustrates a process of preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein;\|[0021] FIGS. 3A- 3Bareflow diagrams that illustratea method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein; and\|[0022] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence\|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS. 3A-3B of the present disclosure according to some embodiments herein.\|DETAILED\|DESCRIPTION OF PREFERRED EMBODIMENTS\|[0023] The embodiments herein and the various features and advantageous details thereof are explained more fully with reference to the non-limiting embodiments that are illustrated in the accompanying drawings and detailed in the following description. Descriptions of well-known components and processing techniques are omitted so as to not unnecessarily obscure the embodiments herein. The examples used herein are intended merely to facilitate an understanding of ways in which the embodiments herein may be practiced and to further enable those of skill in the art to practice the embodiments herein. Accordingly, the examples should not be construed as limiting the scope of the embodiments herein.\|[0024] In the view of the foregoing, the need for a system and methodfor producing carbonate-enhanced nutrition composition using a geo-bag is in the ongoing description.\|Referring now to the drawings, and more particularly to FIGS. 1 through 4D, where similar reference characters denote corresponding features in a consistent manner throughout the figures, there are shown preferred embodiments.\|[0025] FIG. 1 is a block diagram that illustrates a system 100for preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. The system 100 includesa rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The rock crushing unit 102 receives rocks from a source station for compressing and breaking the rocks into small particles. In some embodiments, the source station may be a quarry or a mining area, and the rock is extracted using explosives or mechanical excavators to remove the rock from the ground. The rock crushing unit 102 may include an input unit, a series of crushing and screening units, a transporting unit, and a storage area. The input unit may include a hopper for feeding the rocks and is passed through the series of crushing and screening units for compressing and breaking the rocks into desiredsizes to obtain crushed rocks. The crushed rocks are forwarded to the transporting unit. The transporting unit may include a conveyor belt that carries the crushed rocks to the storage area or an end location. In some embodiments, the crushing and screening unit includes but is not limited to a jaw crusher, a cone crusher, an impact crusher, a gyratory crusher, a ball mill crusher, a feeder breaker, a roll crusher, or a combination thereof.\|[0026] The reactor 108 is connected to the rock crushing unit 102 for receiving the smaller particles of crushed rocks. The urban organic wastage collection unit 104 receives municipal waste and is connected to the organic acid extraction unit 106 to produce organic acidcomponents through an electro-microbial process (EMP). The urban organic wastage collection unit 104 collects and stores organic waste, including municipal solid waste, industrial organic wastes, and or agricultural wastes to produce a biomass material. The biomass material may be produced using a microbial technique.\|[0027] The reactor 108 is connected to the organic acid extraction unit 106 to mix the organic acid componentthat is extracted from a biomass materialwith the crushed rocks to prepare a carbon-sequestration substrate. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere. In some embodiments, the organic acid component is extracted by a liquefaction reaction of biomass under supercritical conditions. The liquefaction reaction of biomass under supercritical conditions results in an effective decomposition of biomass. The supercritical condition may include the addition of water to the biomass and increasing its temperature above the boiling point of the water at which the water has a high pressure and high concentration of H+ and OH- ions. Such supercritical conditions help the conversion of liquefied biomass into cellulose-derived monosaccharides. The cellulosederived monosaccharide is degraded into some short-chain intermediates in the absence of oxidant to produce value-added chemicals that includethe organic acid components. The organic acid components may include but are not limited to acetic acid, citric acid, 2,5-diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid or 2,5-furandicarboxylic acid (FDCA).\|[0028] The reactor 108 is configured for mixing about 70% to 90% of weight/weight\|(w/w) of the crushed rocks and about 10% to 30% weight/volume (w/V) of the organic acid components to prepare a carbon-sequestration substrate at a predetermined mixing condition.\|The predetermined mixing condition may include a mixing temperature ranging from 25°C to\|30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over 2 hours - 48 hours to prepare thecarbon-sequestration substrate.\|[0029] The geo-bag 112 receives the carbon-sequestration substrate from the reactor 108\|through a spray head. The carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and has a pH value ranging from 2.5 to 3.5.\|[0030] The conveyor unit 110 is configured for carrying the carbon-sequestration substrate to a filling station from the reactor 108. The filling station is provided with the geo-bag\|112. In some embodiments, the geo-bag 112 is made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 112. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE),or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3 millimeters (mm). The geo-bag 112 is made from eco-friendly materials that do not decompose over the rock carbonation period, allow selective exchange of material between the bag contents and the environment, and allow retrieval of crushed rock post the carbonation period.\|[0031] The geo-bag 112 is filled with the carbon-sequestration substrate to prepare a carbon-sequestration package. In some embodiments, the geo-bag 112 is filled by dispensing the carbon-sequestration substratethrough a sand spray head that is arranged in the reactor 108. The dispensation of the carbon-sequestration substrateis controlled from the reactor 108 in the thickness of 1 cm to 12 inches at rates of 40-200 tons/hr.\|[0032] The carbon-sequestration packages are transferred to an operating location using a transportation medium. The transportation medium may be a conveyor belt, truck, or manual process.\|[0033] The carbon-sequestration packages are allowed for a rock carbonation period in the operating location by stacking or burying the packages in the operating location. The rock carbonation period may be 2-5 years. The carbon-sequestration substratein a package is enabled to capture the carbon dioxide from the atmosphere and convert thecarbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Thereby, the concentration level of\|CO2 in the atmosphere is reduced. The carbonate-enhanced nutrition compositionincludes high economic value materials, including but not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0034] FIG. 2 illustrates a process 200 for preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein. The process 200 includes a stone crusher 202, a sand grinding ball mill 204, a conveyor unit 206, and a geo-bag 208. The stone crusher 202includes a series of cone crushing units and an automatic feeding arrangement for receiving rock from a source station (e.g.mining area or quarry)for compressing and breaking the rocks into small particles to obtain crushed rocks. The sand grinding ball mill 204 receives the crushed rocks from thestone crusher 202 and mixes the crushed rocks with an organic acid component at a predetermined mixing condition to prepare a carbon-sequestration substrate. The organic acid component is extracted from biomass using an organic acid extraction unit. The conveyor unit 206 carries the carbon-sequestration substrateto a filling station from the sand grinding ball mill 204. The filling station is provided withthe geo-bag 208, whichis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 208. The geo-bag 208 is filled with the carbon-sequestration substrateto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportationmedium. The packages are stacked or buried fora rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere resulting in the conversion of the carbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Such carbonate-enhanced nutrition composition includes high economic value materials including but not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0035] FIGS. 3A-3B are flow diagrams that illustrate a method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. At step\|302, the method includes receiving the rocks from the ground and preparing the crushed rocks by compressing and breaking the rocks into small particles using the rock crushing unit. The crushed rocks include a particle size below 5 mm.\|[0036] At step 304, the method includes collecting and storing organic wastes using the urban organic waste collection unit to produce biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof. The biomass material may be produced using a microbial technique.\|[0037] At step 306, the method includes extracting an organic acid component from the biomass using the organic acid extraction unit. The organic acid component may be extracted using an electro-microbial production (EMP) technique. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketogluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-\|Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere.\|[0038] At step 308, the method includes mixing the crushed rocks in a concentration ranging from 70% to 90% of weight/weight (w/w) and the organic acid component in a concentration ranging from 10% to 30% weight/volume (w/V) to prepare a carbon-sequestration substrate at a predetermined mixing condition using the reactor. The predetermined mixing condition may include a mixing temperature ranging from 25°C to 30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over a few hours to a few days of the period to prepare the carbon-sequestration substrate. In some embodiments, the carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and pH value ranging from 2.5 to 3.5.\|[0039] At step 310, the method includes preparing the geo-bagusing an eco-friendly material that allows selective exchange of material between the bag contents and the environment. The geo-bag does not decompose over the rock carbonation period and allows retrieval of a carbonate-enhanced nutrition composition during the carbonation period. The geo20\|bagis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE), or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3\|millimeters (mm).\|[0040] At step 312, the method includes filling the carbon-sequestration substrate, using a sand spray head arranged in the reactor, into the geo-bagto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportation medium.\|The transportation medium may be a conveyor belt, a truck, or a manual process.\|[0041] At step 314, the method includes allowing the carbon-sequestration packages at a rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere. The packages are stacked or buried in the operating location at the rock carbonation period to capture the carbon dioxide from the atmosphere, resulting in the conversion of the carbon-sequestration substrate into a carbonate-enhanced nutrition composition, thereby reducing environmental CO2 level in the atmosphere. The rock carbonation period may include\|2-5 years. In some embodiments, the operating location is a forming land, construction site, or any other outdoor environment. The carbonate-enhanced nutrition composition is further processed to extract high economic value materials, including but are not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0042] TABLE 1 illustrates an approximate concentration level of high-value materials present in the carbonate-enhanced nutrition composition prepared using the method as described in FIG. 3 of the proposed disclosure.\|[0043] TABLE 1:\|Material Concentration level in percentage\|Potassium (K2O) 0.2 %\|Phosphate (P2O5) 0.4%\|Chromium 0.7%\|Nickel 0.7%\|CaCO3 4%\|[0044] TABLE 2 illustrates experimental results validating the efficiency of the carbonate-enhanced nutrition composition prepared using the method described in FIG. 3 of the present disclosure. The experiments are conducted to accelerate carbonation within a controlled environment, optimizing specific parameters to enhance carbon sequestration efficiency. The study evaluates carbonation performance under varying pH levels and particle sizes to identify the most effective conditions for CO₂ mineralization.\|[0045] TABLE 2:\|Samples\|Carbonization efficiency (%)\|Experiment A\|pH - 2.5 to 3.5\|Rock Size - < 5 mm\|Experiment B\|pH - 6.0 to 6.5\|rock - < 300 microns\|Dunite 60.77 22.7\|Basalt 14.33 7.5\|[0046] The above tabulation shows the experimental setup includes two different conditions: Experiment A is conducted at a pH range of 2.5 to 3.5 with crushed rock samples of less than 5 mm, while Experiment B is conducted at a pH range of 6.0 to 6.5 with a finer particle size of less than 300 microns. The process is carried out within a temperature range of 25°C to\|30°C, in a background bath of acetic acid, ensuring an optimized environment for carbonation.\|[0047] The results demonstrated significant differences in carbonation efficiency between the two experimental setups. Dunite samples exhibited a carbonation efficiency of\|60.77% in Experiment A (pH 2.5 to 3.5, rock size <5 mm), and the efficiency dropped to 22.7%\|in Experiment B (pH 6.0 to 6.5, rock size<300 microns). Similarly, basalt samples showed a carbonation efficiency of 14.33% in Experiment A, which reduced to 7.5% in Experiment B. The experimental results demonstrate that lower pH values and larger particle sizes enhanced carbonation particularly at the optimized conditions including pH 2.5 to 3.5 and the rock size is\|<5 mm.\|[0048] The experiment resultsdemonstrate that the carbonation efficiency is increased 15\|to 130 times higher thanthe natural carbonation process with the optimized conditions, including pH value ranging from 2.5 to 3.5 and the rock Size, includes less than 5 mm. These results validate the technical feasibility and efficiency gains of the method described in FIG. 3 of the proposed disclosure, confirming that the integration of crushed ultramafic and basaltic rocks, organic acid-based substrates, and a controlled carbonation process significantly enhances CO₂\|capture and mineralization efficiency.\|[0049] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence\|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3Bof the present disclosure according to some embodiments herein. The analysis shows the elemental compositions of dunite and basalt samples before and after carbonization process. FIGS. 4A - 4B are graphical representations illustrating the X-ray fluorescence (XRF) analysis of dunite rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the duniterock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw dunite rock samples; (iv) A - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out at the optimized condition including pH 2.5 to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5\|and the rock size including <300 microns. The results indicate that dunite samples subjected to carbonization under optimized conditions (pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw dunite samples and those carbonized under non-optimized conditions (pH 6.0-6.5, rock size <300 microns).\|[0050] FIGS. 4C - 4D are graphical representations illustrating the X-ray fluorescence\|(XRF) analysis of basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the basalt rock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw basalt rock samples; (iv) A - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out at the optimized condition including pH 2.5\|to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5 and the rock size including <300 microns.\|The results indicate that basalt samples subjected to carbonization under optimized conditions\|(pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw basalt samples and those carbonized under non-optimized conditions (pH 6.0-\|6.5, rock size <300 microns). The higher retention and conversion efficiency of valuable elements under optimized carbonation conditions confirm that the process facilitates effective mineralization and enhances sequestration efficiency.\|[0051] The foregoing description of the specific embodiments will so fully reveal the general nature of the embodiments herein that others can, by applying current knowledge, readily modify and/or adapt for various applications such specific embodiments without departing from the generic concept, and, therefore, such adaptations and modifications should and are intended to be comprehended within the meaning and range of equivalents of the disclosed embodiments.\|It is to be understood that the phraseology or terminology employed herein is for the purpose of description and not of limitation. Therefore, while the embodiments herein have been described in terms of preferred embodiments, those skilled in the art will recognize that the embodiments herein can be practiced with modification within the spirit and scope.	(IN202441017388)\|Technical Field\|[0001] The embodiments herein generally relate toa carbon mineralization method, and more particularly, a system and method for preparing carbonate-enhanced nutrition composition using a geo-bag. Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.\|Description of the Related Art\|[0002] In recent years, the significantriseinatmospheric carbon dioxide (CO2) levels has been identified as a leading cause of climate change on Earth. To mitigate this issue, carbon mineralization, or carbon sequestration, has emerged as a prominent method. Carbon mineralization is a process of converting carbon dioxide into solid minerals, such as carbonate, through a chemical reaction. This reaction occurs when specific types of rocks, such as serpentine, basalt, mafic, ultramafic, etc., are exposed to carbon dioxide, resulting in the formation of carbonate-enhanced minerals. Hence, the atmospheric CO2 level is stabilized asthe reacted carbon remains bound within the solid minerals, preventing its release into the atmosphere. However, it is important to note that this process typically requires several years to effectively reduce carbon levels in the atmosphere.\|[0003] Most of the existing carbon sequestration systemsto produce carbonate-enhanced mineralsutilize indoor techniques, employingan indirect method. For example, thesesystemsincludea mineral dissolution reactor for mixing various materials. These materials include magnesium or calcium, which is available in the rocks (e.g. serpentine, olivine, basalt, or labradorite), organic acid, and chelating agents. Through this mixing process, a magnesium or calcium-rich solvent is synthesized tocapture and store carbon dioxide. Additionally, these existing systemsinclude a combined biocatalyst and carbonation reactor, along witha control module for expediting the process of sequestration of carbon. However, the current indoor technique requires a more complicated arrangement and entails higher costs.\|[0004] Accordingly, there remains a need for a more simple and direct approach to capture and store the carbon dioxide from the atmosphere at a reduced economic level and to produce a carbonated enhanced nutrition composition using a geo-bag.\|SUMMARY\|[0005] In view of a foregoing, an embodiment herein provides a method for preparing a carbonate-enhanced nutrition composition using a geo-bag. The method includes i) collecting and crushing rocks into small particles, using a rock crushing unit; ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbonsequestration substrate using a reactor by mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions. The carbon-sequestration substrate is filled into geo-bags to prepare carbon-sequestration packages. The geo-bag includes an eco-friendly material that only permits water and air to pass through while retaining the substrate. The geo-bag consists of a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbon-sequestration substrate by subjecting the carbonsequestration packages to a rock-carbonation period at an operating location to capture atmospheric carbon dioxide. The geo-bag acts as a structural member providing a high surface area-to-volume ratio to optimize carbon dioxide capture resulting in 15 to 130 times enhanced carbonation efficiency.\|[0006] In some embodiments, the crushed rocks include at least one of olivine, dunite, ultramafic, basalt, serpentine, and/or a combination thereof. The crushed rocks include a particle size below 5 mm.\|[0007] In some embodiments, the predefined mixing conditions include a mixing temperature ranging from 25°C to 30°C and an atmospheric pressure ranging from 1 atm to 2\|atm.\|[0008] In some embodiments, the carbon-sequestration substrate includes a concentration level ranging from 400 parts per million (ppm) to 450 ppm, a moisture content ranging from\|25% to 95% of rock weight and a pH value ranging from 2.5 to 3.5.\|[0009] In some embodiments, the geo-bag includes at least one of the geotextiles, highdensity polyethylene (HDPE), and/or a combination thereof.\|[0010] In some embodiments, the rock-carbonation period ranges from 2 years to 5 years.\|[0011] In some embodiments, the organic acid component is extracted using an electromicrobial production (EMP) technique from the biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof.\|[0012] In some embodiments, the operating location includes at least one farming land, a construction site, and an outdoor environment.\|[0013] In some embodiments, the method includes extracting high-value materials from the carbonate-enhanced nutrition composition, wherein the high-value materials include at least one of magnesium carbonate, calcium carbonate, potash, phosphate, heavy metals, and/or a combination thereof.\|[0014] In some embodiments, the carbonate-enhanced nutrition composition is used as fertilizer in agriculture and/or as M-sand in the construction field.\|[0015] . In some embodiments, the refill docking platform includes a connection part that is configured to hold the refill cartridge in an invertedly upright position to enable the flow of the substance from the refill cartridge to the bottom of the primary compartment.\|[0016] The method of preparing a carbonate-enhanced nutrition composition of the present description includes a more direct approach for capturing and storing carbon dioxide from the atmosphere using the geo-bag. The direct approach represents the geo-bag that includes a simple configuration used in an outdoor environment for capturing and storing carbon dioxide from the atmosphere. Such a simple configuration of geo-bag eliminates the need for a complicated arrangement of the carbon dioxide sequestration system used in the existing system.\|The geo-bag includes improved measurement, reporting, and verification (MRV) by enclosing the first mixture in a high surface area to volume ratio and staking in vertical layers to hold the first mixture, and the geo-bag acts as a structural member to produce a carbonate enhanced nutrition composition at a lower economical level. Such carbonate-enhanced nutrition composition includes high economic value materials, which can be used as a fertilizer for agricultural fields or building construction material, e.g. M-sand.\|[0017] These and other aspects of the embodiments herein will be better appreciated and understood when considered in conjunction with the following description and the accompanying drawings. It should be understood, however, that the following descriptions, while indicating preferred embodiments and numerous specific details thereof, are given by way of illustration and not of limitation. Many changes and modifications may be made within the scope of the embodiments herein without departing from the spirit thereof, and the embodiments herein include all such modifications.\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] The embodiments herein will be better understood from the following detailed description with reference to the drawings, in which:\|[0019] FIG. 1 is a block diagram that illustrates a systemforpreparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein;\|[0020] FIG. 2 illustrates a process of preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein;\|[0021] FIGS. 3A- 3Bareflow diagrams that illustratea method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein; and\|[0022] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence\|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS. 3A-3B of the present disclosure according to some embodiments herein.\|DETAILED\|DESCRIPTION OF PREFERRED EMBODIMENTS\|[0023] The embodiments herein and the various features and advantageous details thereof are explained more fully with reference to the non-limiting embodiments that are illustrated in the accompanying drawings and detailed in the following description. Descriptions of well-known components and processing techniques are omitted so as to not unnecessarily obscure the embodiments herein. The examples used herein are intended merely to facilitate an understanding of ways in which the embodiments herein may be practiced and to further enable those of skill in the art to practice the embodiments herein. Accordingly, the examples should not be construed as limiting the scope of the embodiments herein.\|[0024] In the view of the foregoing, the need for a system and methodfor producing carbonate-enhanced nutrition composition using a geo-bag is in the ongoing description.\|Referring now to the drawings, and more particularly to FIGS. 1 through 4D, where similar reference characters denote corresponding features in a consistent manner throughout the figures, there are shown preferred embodiments.\|[0025] FIG. 1 is a block diagram that illustrates a system 100for preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. The system 100 includesa rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The rock crushing unit 102 receives rocks from a source station for compressing and breaking the rocks into small particles. In some embodiments, the source station may be a quarry or a mining area, and the rock is extracted using explosives or mechanical excavators to remove the rock from the ground. The rock crushing unit 102 may include an input unit, a series of crushing and screening units, a transporting unit, and a storage area. The input unit may include a hopper for feeding the rocks and is passed through the series of crushing and screening units for compressing and breaking the rocks into desiredsizes to obtain crushed rocks. The crushed rocks are forwarded to the transporting unit. The transporting unit may include a conveyor belt that carries the crushed rocks to the storage area or an end location. In some embodiments, the crushing and screening unit includes but is not limited to a jaw crusher, a cone crusher, an impact crusher, a gyratory crusher, a ball mill crusher, a feeder breaker, a roll crusher, or a combination thereof.\|[0026] The reactor 108 is connected to the rock crushing unit 102 for receiving the smaller particles of crushed rocks. The urban organic wastage collection unit 104 receives municipal waste and is connected to the organic acid extraction unit 106 to produce organic acidcomponents through an electro-microbial process (EMP). The urban organic wastage collection unit 104 collects and stores organic waste, including municipal solid waste, industrial organic wastes, and or agricultural wastes to produce a biomass material. The biomass material may be produced using a microbial technique.\|[0027] The reactor 108 is connected to the organic acid extraction unit 106 to mix the organic acid componentthat is extracted from a biomass materialwith the crushed rocks to prepare a carbon-sequestration substrate. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere. In some embodiments, the organic acid component is extracted by a liquefaction reaction of biomass under supercritical conditions. The liquefaction reaction of biomass under supercritical conditions results in an effective decomposition of biomass. The supercritical condition may include the addition of water to the biomass and increasing its temperature above the boiling point of the water at which the water has a high pressure and high concentration of H+ and OH- ions. Such supercritical conditions help the conversion of liquefied biomass into cellulose-derived monosaccharides. The cellulosederived monosaccharide is degraded into some short-chain intermediates in the absence of oxidant to produce value-added chemicals that includethe organic acid components. The organic acid components may include but are not limited to acetic acid, citric acid, 2,5-diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid or 2,5-furandicarboxylic acid (FDCA).\|[0028] The reactor 108 is configured for mixing about 70% to 90% of weight/weight\|(w/w) of the crushed rocks and about 10% to 30% weight/volume (w/V) of the organic acid components to prepare a carbon-sequestration substrate at a predetermined mixing condition.\|The predetermined mixing condition may include a mixing temperature ranging from 25°C to\|30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over 2 hours - 48 hours to prepare thecarbon-sequestration substrate.\|[0029] The geo-bag 112 receives the carbon-sequestration substrate from the reactor 108\|through a spray head. The carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and has a pH value ranging from 2.5 to 3.5.\|[0030] The conveyor unit 110 is configured for carrying the carbon-sequestration substrate to a filling station from the reactor 108. The filling station is provided with the geo-bag\|112. In some embodiments, the geo-bag 112 is made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 112. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE),or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3 millimeters (mm). The geo-bag 112 is made from eco-friendly materials that do not decompose over the rock carbonation period, allow selective exchange of material between the bag contents and the environment, and allow retrieval of crushed rock post the carbonation period.\|[0031] The geo-bag 112 is filled with the carbon-sequestration substrate to prepare a carbon-sequestration package. In some embodiments, the geo-bag 112 is filled by dispensing the carbon-sequestration substratethrough a sand spray head that is arranged in the reactor 108. The dispensation of the carbon-sequestration substrateis controlled from the reactor 108 in the thickness of 1 cm to 12 inches at rates of 40-200 tons/hr.\|[0032] The carbon-sequestration packages are transferred to an operating location using a transportation medium. The transportation medium may be a conveyor belt, truck, or manual process.\|[0033] The carbon-sequestration packages are allowed for a rock carbonation period in the operating location by stacking or burying the packages in the operating location. The rock carbonation period may be 2-5 years. The carbon-sequestration substratein a package is enabled to capture the carbon dioxide from the atmosphere and convert thecarbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Thereby, the concentration level of\|CO2 in the atmosphere is reduced. The carbonate-enhanced nutrition compositionincludes high economic value materials, including but not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0034] FIG. 2 illustrates a process 200 for preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein. The process 200 includes a stone crusher 202, a sand grinding ball mill 204, a conveyor unit 206, and a geo-bag 208. The stone crusher 202includes a series of cone crushing units and an automatic feeding arrangement for receiving rock from a source station (e.g.mining area or quarry)for compressing and breaking the rocks into small particles to obtain crushed rocks. The sand grinding ball mill 204 receives the crushed rocks from thestone crusher 202 and mixes the crushed rocks with an organic acid component at a predetermined mixing condition to prepare a carbon-sequestration substrate. The organic acid component is extracted from biomass using an organic acid extraction unit. The conveyor unit 206 carries the carbon-sequestration substrateto a filling station from the sand grinding ball mill 204. The filling station is provided withthe geo-bag 208, whichis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 208. The geo-bag 208 is filled with the carbon-sequestration substrateto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportationmedium. The packages are stacked or buried fora rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere resulting in the conversion of the carbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Such carbonate-enhanced nutrition composition includes high economic value materials including but not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0035] FIGS. 3A-3B are flow diagrams that illustrate a method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. At step\|302, the method includes receiving the rocks from the ground and preparing the crushed rocks by compressing and breaking the rocks into small particles using the rock crushing unit. The crushed rocks include a particle size below 5 mm.\|[0036] At step 304, the method includes collecting and storing organic wastes using the urban organic waste collection unit to produce biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof. The biomass material may be produced using a microbial technique.\|[0037] At step 306, the method includes extracting an organic acid component from the biomass using the organic acid extraction unit. The organic acid component may be extracted using an electro-microbial production (EMP) technique. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketogluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-\|Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere.\|[0038] At step 308, the method includes mixing the crushed rocks in a concentration ranging from 70% to 90% of weight/weight (w/w) and the organic acid component in a concentration ranging from 10% to 30% weight/volume (w/V) to prepare a carbon-sequestration substrate at a predetermined mixing condition using the reactor. The predetermined mixing condition may include a mixing temperature ranging from 25°C to 30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over a few hours to a few days of the period to prepare the carbon-sequestration substrate. In some embodiments, the carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and pH value ranging from 2.5 to 3.5.\|[0039] At step 310, the method includes preparing the geo-bagusing an eco-friendly material that allows selective exchange of material between the bag contents and the environment. The geo-bag does not decompose over the rock carbonation period and allows retrieval of a carbonate-enhanced nutrition composition during the carbonation period. The geo20\|bagis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE), or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3\|millimeters (mm).\|[0040] At step 312, the method includes filling the carbon-sequestration substrate, using a sand spray head arranged in the reactor, into the geo-bagto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportation medium.\|The transportation medium may be a conveyor belt, a truck, or a manual process.\|[0041] At step 314, the method includes allowing the carbon-sequestration packages at a rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere. The packages are stacked or buried in the operating location at the rock carbonation period to capture the carbon dioxide from the atmosphere, resulting in the conversion of the carbon-sequestration substrate into a carbonate-enhanced nutrition composition, thereby reducing environmental CO2 level in the atmosphere. The rock carbonation period may include\|2-5 years. In some embodiments, the operating location is a forming land, construction site, or any other outdoor environment. The carbonate-enhanced nutrition composition is further processed to extract high economic value materials, including but are not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0042] TABLE 1 illustrates an approximate concentration level of high-value materials present in the carbonate-enhanced nutrition composition prepared using the method as described in FIG. 3 of the proposed disclosure.\|[0043] TABLE 1:\|Material Concentration level in percentage\|Potassium (K2O) 0.2 %\|Phosphate (P2O5) 0.4%\|Chromium 0.7%\|Nickel 0.7%\|CaCO3 4%\|[0044] TABLE 2 illustrates experimental results validating the efficiency of the carbonate-enhanced nutrition composition prepared using the method described in FIG. 3 of the present disclosure. The experiments are conducted to accelerate carbonation within a controlled environment, optimizing specific parameters to enhance carbon sequestration efficiency. The study evaluates carbonation performance under varying pH levels and particle sizes to identify the most effective conditions for CO₂ mineralization.\|[0045] TABLE 2:\|Samples\|Carbonization efficiency (%)\|Experiment A\|pH - 2.5 to 3.5\|Rock Size - < 5 mm\|Experiment B\|pH - 6.0 to 6.5\|rock - < 300 microns\|Dunite 60.77 22.7\|Basalt 14.33 7.5\|[0046] The above tabulation shows the experimental setup includes two different conditions: Experiment A is conducted at a pH range of 2.5 to 3.5 with crushed rock samples of less than 5 mm, while Experiment B is conducted at a pH range of 6.0 to 6.5 with a finer particle size of less than 300 microns. The process is carried out within a temperature range of 25°C to\|30°C, in a background bath of acetic acid, ensuring an optimized environment for carbonation.\|[0047] The results demonstrated significant differences in carbonation efficiency between the two experimental setups. Dunite samples exhibited a carbonation efficiency of\|60.77% in Experiment A (pH 2.5 to 3.5, rock size <5 mm), and the efficiency dropped to 22.7%\|in Experiment B (pH 6.0 to 6.5, rock size<300 microns). Similarly, basalt samples showed a carbonation efficiency of 14.33% in Experiment A, which reduced to 7.5% in Experiment B. The experimental results demonstrate that lower pH values and larger particle sizes enhanced carbonation particularly at the optimized conditions including pH 2.5 to 3.5 and the rock size is\|<5 mm.\|[0048] The experiment resultsdemonstrate that the carbonation efficiency is increased 15\|to 130 times higher thanthe natural carbonation process with the optimized conditions, including pH value ranging from 2.5 to 3.5 and the rock Size, includes less than 5 mm. These results validate the technical feasibility and efficiency gains of the method described in FIG. 3 of the proposed disclosure, confirming that the integration of crushed ultramafic and basaltic rocks, organic acid-based substrates, and a controlled carbonation process significantly enhances CO₂\|capture and mineralization efficiency.\|[0049] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence\|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3Bof the present disclosure according to some embodiments herein. The analysis shows the elemental compositions of dunite and basalt samples before and after carbonization process. FIGS. 4A - 4B are graphical representations illustrating the X-ray fluorescence (XRF) analysis of dunite rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the duniterock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw dunite rock samples; (iv) A - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out at the optimized condition including pH 2.5 to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5\|and the rock size including <300 microns. The results indicate that dunite samples subjected to carbonization under optimized conditions (pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw dunite samples and those carbonized under non-optimized conditions (pH 6.0-6.5, rock size <300 microns).\|[0050] FIGS. 4C - 4D are graphical representations illustrating the X-ray fluorescence\|(XRF) analysis of basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the basalt rock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw basalt rock samples; (iv) A - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out at the optimized condition including pH 2.5\|to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5 and the rock size including <300 microns.\|The results indicate that basalt samples subjected to carbonization under optimized conditions\|(pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw basalt samples and those carbonized under non-optimized conditions (pH 6.0-\|6.5, rock size <300 microns). The higher retention and conversion efficiency of valuable elements under optimized carbonation conditions confirm that the process facilitates effective mineralization and enhances sequestration efficiency.\|[0051] The foregoing description of the specific embodiments will so fully reveal the general nature of the embodiments herein that others can, by applying current knowledge, readily modify and/or adapt for various applications such specific embodiments without departing from the generic concept, and, therefore, such adaptations and modifications should and are intended to be comprehended within the meaning and range of equivalents of the disclosed embodiments.\|It is to be understood that the phraseology or terminology employed herein is for the purpose of description and not of limitation. Therefore, while the embodiments herein have been described in terms of preferred embodiments, those skilled in the art will recognize that the embodiments herein can be practiced with modification within the spirit and scope.	Family Number\|(116031041)\|116031041\|Object of Invention\|(IN202441017388 A)\|Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.\|Abstract\|(IN202441017388 A)\|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112. The system includes a rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The reactor 108 mixes crushed rocks and organic acid components to prepare a carbon-sequestration substrate. The geo-bag 112 is filled with the carbon-sequestration substrate, and the geo-bag 112 is made from eco-friendly materials, allowing selective exchange of components between the bag contents and the environment. The substrate in the geo-bag 112 is allowed to capture the CO2 from the atmosphereand convert the carbon-sequestration substrate into a carbonateenhanced nutrition composition, thereby reducing the environmental CO2 level. The composition includes high economic value materials like calcium carbonate, potash, phosphate, and heavy metals. The composition can be used as a fertilizer or building construction material like M-sand.\|Independent Claims\|(IN202441017388 A)\|1. A method for preparing a carbonate-enhanced nutrition composition using a geo-bag (112) wherein the method comprising: i) Collecting and crushing rocks into small particles, using a rock crushing unit (102); ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbon-sequestration substrate, using a reactor (108) by Characterized in that, a) mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions; and b) filling the carbon-sequestration substrate into the geo-bag (112) to prepare carbon-sequestration packages, wherein the geo-bag (112) comprises an ecofriendly material that permits only water and air to pass through while (...) millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbonsequestration substrate by subjecting the carbon-sequestration packages to a rockcarbonation period at an operating location to capture atmospheric carbon dioxide; wherein the geo-bag (112) acts as a structural member providing a high surface area-tovolume ratio to optimize carbon dioxide capture resulting 15 to 130 times enhanced carbonation efficiency.\|	Other special machines				A01G-024/12\|A01G-024/15\|A01G-024/17\|A01G-024/20\|A01G-024/60	A01G-024/12\|A01G-024/15\|A01G-024/17\|A01G-024/20\|A01G-024/60										PENDING	(IN202441017388)\|PENDING	ALIVE	(IN202441017388)\|ALIVE	(IN202441017388)\|LEGAL DETAILS FOR IN202441017388\|Actual or expected expiration date=2044-03-11\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-11\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN202441017388\|Application date=2024-03-11\|Standardized application number=2024IN-41017388\|Event publication date=2025-09-12\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN202441017388\|Publication stage code=A\|Publication date=2025-09-12\|Standardized publication number=IN202441017388		(IN202441017388)\|IN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=/WizbbSQlgu/uP20qNF3JE9lJnxGv8IZa/WZFbsCsqzB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=IN0000000001670167&ekey=2476&xpn=IN202441017388&kind=A	https://iprsearch.ipindia.gov.in/PublicSearch/PublicationSearch/ApplicationStatus	https://permalink.orbit.com/RenderStaticFirstPage?XPN=dR15du4ks0vl9J154pQkJcExnvIz5kLrfqHome9U%252B8A%3D%26n%3D1&id=0&base=FAMPAT	IN						(IN202441017388)\|NAME=Tannirkulam Ajay\|NAME=Margankunte Naveen	(IN202441017388)\|4	1	1					(IN202441017388)\|Number of Claims: NCL=10\|		(IN202441017388)\|ENGLISH (ENG)	(IN202441017388)\|Patent	Titre: (IN202441017388)\|System and method for preparing carbonate-enhanced nutrition composition using geo-bags Résumé: (IN202441017388)\|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112. The system includes a rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The reactor 108 mixes crushed rocks and organic acid components to prepare a carbon-sequestration substrate. The geo-bag 112 is filled with the carbon-sequestration substrate, and the geo-bag 112 is made from eco-friendly materials, allowing selective exchange of components between the bag contents and the environment. The substrate in the geo-bag 112 is allowed to capture the CO2 from the atmosphereand convert the carbon-sequestration substrate into a carbonateenhanced nutrition composition, thereby reducing the environmental CO2 level. The composition includes high economic value materials like calcium carbonate, potash, phosphate, and heavy metals. The composition can be used as a fertilizer or building construction material like M-sand.	10	Abstract	gpt-4o-mini	yes	The article describes a system for preparing a carbon-sequestration substrate that captures CO₂ and converts it into carbonates, aligning with the topic of enhanced weathering and carbon sequestration.
13	US63/569,558P\|US19/089,278	WOCA2025/050423\|US19/089,278	WO2025/199637\|US20250297409	116035972	WO2025/199637 A1 2025-10-02 [WO2025199637]\|US20250297409 A1 2025-09-25 [US20250297409]	2024-03-25\|2025-03-25	2025-03-25\|2025-03-25	2025-10-02\|2025-09-25		(US20250297409)\|2045-03-25\|(WO2025/199637)\|2027-09-25	(US20250297409)\|Carbon sequestration sand-based material for synthetic turf fields	(US20250297409)\|A synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.	TARKETT SPORTS	(US20250297409)\|Tarkett Sports Canada Inc. ([CA])\|(WO2025/199637)\|TARKETT SPORTS CANADA INC. ([CA])	SMOLETT JASON\|HABIB ERIC\|CHISAM CHRISTOPHER	(US20250297409)\|Smolett Jason\|Habib Eric\|Chisam Christopher	(WO2025/199637)\|YIP, Vincent ([CA])	(US20250297409)\|As will be appreciated, mesh may be defined as the number of openings in one square inch of a screen.\|Furthermore, it will be appreciated that by placing the carbon sequestration sand 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air.\|It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|	(US20250297409)\|1. A synthetic turf system comprising: a backing; turf fibers extended upward from the backing; one or more infill layers positioned above the backing, below a top portion of the turf fibers; wherein the one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|12. Infill for a synthetic turf system, the infill comprising: carbon sequestration sand including silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh; and organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|17. A method of preparing a synthetic turf system, the method comprising: dispersing carbon sequestration sand over a top portion of turf fibers, wherein the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|	(US20250297409)\|According to another aspect, infill for a synthetic turf system includes carbon sequestration sand.\|As used in this application, "or" is intended to mean an inclusive "or" rather than an exclusive "or".\|In accordance with varying embodiments discussed herein, there is provided an artificial turf system that utilizes a material derived from one or more types of carbon sequestration sands, including, for example and without limitation, wollastonite sand (general formula CaSiO_3), limestone, basalt, or the like.\|	(US20250297409)\|CARBON SEQUESTRATION(100,154)\|CARBON SEQUESTRATION SAND(100,44)\|SYNTHETIC TURF FIELD(100,4)\|SAND MATERIAL(100,3)\|CARBON SEQUESTRATION SAND MATERIAL(100,1)\|INFILL LAYER(91,53)\|TURF FIBER(82,33)\|SILICATE ROCK(82,15)\|ROCK REACTION(71,14)\|SYNTHETIC TURF(63,70)\|WOLLASTONITE SAND(52,1)\|BACKING(47,38)\|ULTRAMAFIC ROCK(47,15)\|ELASTOMER PARTICLE(45,4)\|THERMOPLASTIC PARTICLE(43,4)\|BASE ROCK LAYER(41,38)\|RAINWATER(40,24)\|LAYERED INSTALLATION(40,1)\|MESH SCREEN(36,6)\|DISPERSING CARBON SEQUESTRATION(35,2)\|RUBBER PARTICLE(34,4)\|RAIN WATER TRAVEL(32,1)\|BICARBONATE(30,10)\|COATED PARTICLE(30,4)\|ORGANIC PARTICLE(30,4)\|SYNTHETIC TURF BACKING(30,1)\|SYNTHETIC TURF INFILL LAYER(29,1)\|WEATHERED PARTICLE(28,2)\|INFILL(26,10)\|LIMESTONE(26,10)\|CARBON SEQUESTRATION LAYER(26,3)\|BASALT(25,8)\|SUBGRADE(23,9)\|TURF FIBER ANDTHE TOP(23,1)\|ARTIFICIAL TURF(22,2)\|PERIDOTITE(21,4)\|TURF(20,3)\|DUNITE(19,4)\|SPHERICITY(16,3)\|INFILL LAYER THICKNESS(16,2)\|POROSITY(13,2)\|GROUND(12,3)\|CARBONATE SEDIMENT(11,3)\|TURF CARPET(11,2)\|SHOCK PAD(10,6)\|CARBON SEQUESTRATION SAND INFILL(10,2)\|DRAINAGE STONE(10,2)\|OLIVINE(9,8)\|ROCK COMPACTION(9,2)\|HARDWOOD SAPWOOD(9,1)\|GEOTEXTILE COMPONENT(8,4)\|CONJOINED CLAUSE(8,1)\|SUBDRAIN TRENCH COMPONENT STONE(8,1)\|TURF FIBER STABILIZATION(8,1)\|CARBON DIOXIDE(7,10)\|PARTICLE SIZE(7,6)\|ARTIFICIAL GRASS BLADE(7,2)\|DRAINAGE PIPE(7,2)\|AERIAL SPREADER(7,1)\|ARTIFICIAL TURF INFILL(7,1)\|BALLAST INFILL(7,1)\|COMPACTION VARIABILITY(7,1)\|HANDHELD SPREADER(7,1)\|INFILL MIGRATION(7,1)\|LAYMOR BRUSH(7,1)\|PROPYLENE DIENE MONOMER(7,1)\|TURF BRUSHING EQUIPMENT(7,1)\|COMPACTED STONE BASE(6,2)\|DEACIDIFYING(6,2)\|HOPPER GATE(6,2)\|BROADCASTER TOOL(6,1)\|COCONUT PEAT(6,1)\|ENDPOINT RECITATION(6,1)\|OLIVE PIT(6,1)\|OSCILLATING BRUSH(6,1)\|PARTICLE SIZING(6,1)\|PERMEABLE BACKING(6,1)\|PNEUMATIC SPREADER(6,1)\|REGULAR DRAINAGE MEASURE(6,1)\|SEED TENDER(6,1)\|WALK BEHIND ROTARY BRUSH(6,1)\|CARBONIC ACID(5,6)\|MESH SIZE(5,4)\|CARBON SEQUESTRATION SAND LAYER(5,3)\|TRACTION(5,3)\|AIR BOOM SPREADER(5,1)\|BALL INTERACTION(5,1)\|HYDRAULIC BRUSH(5,1)\|INFILL LAYER REMAINDER(5,1)\|SYNTHETIC TURF ENVIRONMENTAL SUSTAINABILITY(5,1)\|TRIANGULAR BRUSH(5,1)\|COMPOSITIONAL RANGE(4,4)\|RIVER(4,4)\|SEA(4,4)\|BALLAST LAYER(4,2)\|BICARBONATE SOLUTION(4,2)\|DOLOMITE(4,2)\|DURABILITY(4,2)\|GRANITE(4,2)\|HYDRAULICALLY CONTROLLED CONVEYER(4,2)\|MINERAL NUTRIENT(4,2)\|STORM WATER(4,2)\|THERMOPLASTIC(4,2)\|BICARBONATE FORMATION(4,1)\|DESCRIPTOR(4,1)\|FLEXIBLE BRUSH(4,1)\|NATURAL GRASS BLADE(4,1)\|PACKING STABILITY(4,1)\|PARTICLE ETHYLENE(4,1)\|PUNCHED HOLE(4,1)\|RAIN WATER REACTION(4,1)\|RIGID BRUSH(4,1)\|ROTARY BRUSH ACTION(4,1)\|STRAIGHT BRUSH(4,1)\|SYNTHETIC TURF CAPACITY(4,1)\|SYNTHETIC TURF MANUFACTURING(4,1)\|STONE BASE LAYER(3,3)\|BAMBOO(3,1)\|CARBON CAPTURE BENEFIT(3,1)\|CARBON DIOXIDE DISSOLUTION(3,1)\|CARBONACEOUS MINERAL MATERIAL(3,1)\|CYPRESS(3,1)\|ELASTOMER(3,1)\|ENGINEERING(3,1)\|ENVIRONMENTALLY FRIENDLY(3,1)\|EQUILIBRIUM(3,1)\|EXHIBIT SUPERIOR MECHANICAL PERFORMANCE(3,1)\|GRAINING(3,1)\|GROOMER(3,1)\|HEARTWOOD(3,1)\|IDENTIFICATION(3,1)\|INFILL ARRANGEMENT(3,1)\|INFILL LAYER MINIMUM VOLUME(3,1)\|\|(WO2025/199637)\|CARBON SEQUESTRATION(100,154)\|SYNTHETIC TURF(100,71)\|CARBON SEQUESTRATION SAND(100,44)\|SAND MATERIAL(100,3)\|CARBON SEQUESTRATION SAND MATERIAL(100,1)\|SILICATE ROCK(88,15)\|INFILL LAYER(87,53)\|TURF FIBER(84,33)\|ROCK REACTION(77,14)\|DISPERSING CARBON SEQUESTRATION(55,2)\|ULTRAMAFIC ROCK(51,15)\|BACKING(45,38)\|RAINWATER(43,24)\|ELASTOMER PARTICLE(43,4)\|THERMOPLASTIC PARTICLE(42,4)\|BASE ROCK LAYER(39,38)\|LAYERED INSTALLATION(38,1)\|BICARBONATE(36,10)\|MESH SCREEN(34,6)\|INFILL(32,11)\|RUBBER PARTICLE(32,4)\|RAIN WATER TRAVEL(31,1)\|COATED PARTICLE(29,4)\|ORGANIC PARTICLE(29,4)\|SUBGRADE LAYER(29,1)\|SYNTHETIC TURF BACKING(29,1)\|SYNTHETIC TURF INFILL LAYER(28,1)\|WEATHERED PARTICLE(27,2)\|ENVIRONMENTALLY FRIENDLY(26,1)\|CARBON SEQUESTRATION LAYER(25,3)\|TRANSPORTATION(25,1)\|GEOTEXTILE(22,2)\|PERIDOTITE(20,4)\|TURF(19,3)\|LIMESTONE(18,10)\|DUNITE(18,4)\|BASALT(17,8)\|CARBON OFFSETTING(16,1)\|CARBON OFFSETTING INFILL MATERIAL(16,1)\|SPHERICITY(15,3)\|INFILL LAYER THICKNESS(15,2)\|POROSITY(13,2)\|CARBON NEUTRAL(13,1)\|INFILL MATERIAL(11,9)\|TURF CARPET(11,2)\|SHOCK PAD(10,6)\|CARBON SEQUESTRATION SAND INFILL(10,2)\|DRAINAGE STONE(10,2)\|HARDWOOD SAPWOOD(9,1)\|MECHANICAL RESISTANCE(9,1)\|OLIVINE(8,8)\|GEOTEXTILE COMPONENT(8,4)\|MECHANICAL PROPERTY(8,3)\|ROCK COMPACTION(8,2)\|CONJOINED CLAUSE(8,1)\|SUBDRAIN TRENCH COMPONENT STONE(8,1)\|TURF FIBER STABILIZATION(8,1)\|PARTICLE SIZE(7,6)\|ARTIFICIAL GRASS BLADE(7,2)\|DRAINAGE PIPE(7,2)\|AERIAL SPREADER(7,1)\|ARTIFICIAL TURF INFILL(7,1)\|BALLAST INFILL(7,1)\|COMPACTION VARIABILITY(7,1)\|HANDHELD SPREADER(7,1)\|INFILL MIGRATION(7,1)\|LAYMOR BRUSH(7,1)\|TURF BRUSHING EQUIPMENT(7,1)\|SEDIMENT(6,4)\|BROADCASTER TOOL(6,1)\|COCONUT PEAT(6,1)\|ENDPOINT RECITATION(6,1)\|OLIVE PIT(6,1)\|OSCILLATING BRUSH(6,1)\|PARTICLE SIZING(6,1)\|PERMEABLE BACKING(6,1)\|PNEUMATIC SPREADER(6,1)\|REGULAR DRAINAGE MEASURE(6,1)\|SEED TENDER(6,1)\|WALK BEHIND ROTARY BRUSH(6,1)\|WOLLASTONITE SAND(6,1)\|CARBONIC ACID(5,6)\|MESH SIZE(5,4)\|TRACTION(5,3)\|COMPACTED STONE BASE(5,2)\|DEACIDIFYING(5,2)\|HOPPER GATE(5,2)\|AIR BOOM SPREADER(5,1)\|BALL INTERACTION(5,1)\|COM COB(5,1)\|FORMULA CASIO(5,1)\|HIGH AVAILABILITY(5,1)\|HYDRAULIC BRUSH(5,1)\|INFILL LAYER REMAINDER(5,1)\|SYNTHETIC TURF ENVIRONMENTAL SUSTAINABILITY(5,1)\|TRIANGULAR BRUSH(5,1)\|COMPOSITIONAL RANGE(4,4)\|RIVER(4,4)\|SEA(4,4)\|BALLAST LAYER(4,2)\|BICARBONATE SOLUTION(4,2)\|CARBON SEQUESTRATION SAND LAYER(4,2)\|DOLOMITE(4,2)\|DURABILITY(4,2)\|GRANITE(4,2)\|HYDRAULICALLY CONTROLLED CONVEYER(4,2)\|MINERAL NUTRIENT(4,2)\|STORM WATER(4,2)\|THERMOPLASTIC(4,2)\|DESCRIPTOR(4,1)\|FLEXIBLE BRUSH(4,1)\|NATURAL GRASS BLADE(4,1)\|PACKING STABILITY(4,1)\|PUNCHED HOLE(4,1)\|RAIN WATER REACTION(4,1)\|RIGID BRUSH(4,1)\|ROTARY BRUSH ACTION(4,1)\|STRAIGHT BRUSH(4,1)\|SYNTHETIC TURF CAPACITY(4,1)\|SYNTHETIC TURF MANUFACTURING(4,1)\|CARBON DIOXIDE(3,10)\|GROUND(3,3)\|STONE BASE LAYER(3,3)\|BAMBOO(3,1)\|CARBON CAPTURE BENEFIT(3,1)\|CARBONACEOUS MINERAL MATERIAL(3,1)\|CYPRESS(3,1)\|ELASTOMER(3,1)\|ENGINEERING(3,1)\|EQUILIBRIUM(3,1)\|EXHIBIT SUPERIOR MECHANICAL PERFORMANCE(3,1)\|GRAINING(3,1)\|GROOMER(3,1)\|HEARTWOOD(3,1)\|IDENTIFICATION(3,1)\|	(US20250297409)\|1. A synthetic turf system comprising:\| a backing;\| turf fibers extended upward from the backing;\| one or more infill layers positioned above the backing, below a top portion of the turf fibers;\| wherein the one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|2. The synthetic turf system of claim 1, wherein the carbon sequestration sand includes wollastonite, basalt, peridotite, dunite, limestone, or dolostone.\|3. The synthetic turf system of claim 1, wherein the carbon sequestration sand is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the carbon sequestration sand chemically react with each other, forming a carbonate or a bicarbonate.\|4. The synthetic turf system of claim 1, wherein the carbon sequestration sand has a particle size of about #4 mesh to about #270 mesh, and is deposited in a layer having a thickness of about 1/16 to about ¼ inches above or below each of the one or more infill layers.\|5. The synthetic turf system of claim 1, wherein 90 percent of the carbon sequestration sand is small enough to pass through a #40 mesh screen, but too large to pass through an #80 mesh screen.\|6. The synthetic turf system of claim 1, wherein the one or more infill layers include the carbon sequestration sand,\| the one or more infill layers are disposed on top of the backing, between the turf fibers, and\| the top portion of the turf fibers extends above the one or more infill layers.\|7. The synthetic turf system of claim 1, wherein the backing is water permeable with a porosity that filters rainwater from the carbon sequestration sand and the one or more infill layers by gravity as the rainwater travels from the one or more infill layers to below the backing.\|8. The synthetic turf system of claim 1, further comprising a first base stone layer disposed below the backing, and a second base stone layer disposed below the first base stone layer, wherein the first base stone layer or the second base stone layer includes silicate rock, ultramafic rock, or reactive rock that is accessible to rainwater by gravity from the top portion of the turf fibers.\|9. The synthetic turf system of claim 8, wherein the carbon sequestration sand is positioned on, above, or in the first base stone layer or the second base stone layer.\|10. The synthetic turf system of claim 8, wherein the carbon sequestration sand is positioned below the second base stone layer, tilled into a subgrade below the second base stone layer, or positioned in a subdrain below the second base stone layer.\|11. The synthetic turf system of claim 8, wherein the first base stone layer or the second base stone layer is water permeable, and the carbon sequestration sand is blended into the first base stone layer or the second base stone layer.\|12. Infill for a synthetic turf system, the infill comprising:\| carbon sequestration sand including silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh; and\| organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|13. The carbon sequestration sand of claim 12, wherein 90 percent of the carbon sequestration sand is small enough to pass through a #40 mesh screen.\|14. The carbon sequestration sand of claim 13, wherein 90 percent of the carbon sequestration sand is too large to pass through an #80 mesh screen.\|15. The carbon sequestration sand of claim 12, wherein the silicate rock, ultramafic rock, or reactive rock is at least one of wollastonite, basalt, peridotite, dunite, limestone, and dolostone.\|16. The carbon sequestration sand of claim 12, wherein the silicate rock, ultramafic rock, or reactive rock forms weathered particles having a sphericity of about 0.65 to about 0.85.\|17. A method of preparing a synthetic turf system, the method comprising:\| dispersing carbon sequestration sand over a top portion of turf fibers, wherein the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|18. The method of claim 17, further comprising:\| grooming the carbon sequestration sand into the one or more infill layers of the synthetic turf system, between the turf fibers, at a backing of the synthetic turf system.\|19. The method of claim 17, further comprising:\| preblending the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the carbon sequestration sand over the top portion of the turf fibers.\|20. The method of claim 17, further comprising:\| measuring an aspect of the synthetic turf system, including a thickness of an infill layer, an acidity of rainwater at the infill layer, or a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer; and\| dispersing a predetermined quantity of the carbon sequestration sand over the top portion of the turf fibers as a top dressing based on the measured aspect.	(US20250297409)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] The application claims priority to and the benefit of U.S. Provisional Patent Application No. 63/569,558, filed on Mar. 25, 2024, entitled “Carbon Capture System and Method for Synthetic Turf Fields”, which we incorporate by reference in its entirety.\|(US20250297409)\|BACKGROUND\|[0002] Artificial or synthetic turf fields are composed of three primary components—from bottom to top: shock pad, carpet, and infill. These components are generally assembled on top of a base of compacted stone. The shock pad is optional and serves to convey much of the shock absorption performance of the turf field, required for the safety of those playing on the surface in the case of impact with the surface. The carpet serves to mimic the blades of grass and root zone, conveying the softness and traction of the surface as well as many of the ball interaction properties. The infill is generally constituted of at least two layers, the bottom layer of which serves to weight down and stabilize the carpets that it is laid onto, whereas the top layers serve as an additional interface layer to those playing on the field, conveying surface softness, friction, traction, and much of the mechanical properties of the field that are felt directly by the players.\|[0003] As a matter of background, a significant amount of engineering and development is devoted to developing artificial turf field systems. With respect to the infill, each kind of material has its own performance and structural characteristics. Obtaining the right composition and arrangement of materials can be challenging.\|[0004] Furthermore, when installation of a synthetic turf field occurs, generally speaking, a living, natural turf field is being replaced with an artificial one. In this process, a living organism, e.g., grass, plants, etc., which naturally removes carbon dioxide from the atmosphere is removed. Additionally, the construction associated with a synthetic turf field, as well as the actual manufacturing of the synthetic turf, result in additional carbon entering the atmosphere.\|[0005] As such, there remains a need for environmentally friendly and ultimately carbon-neutral or carbon-offsetting infill materials that present good mechanical properties and mechanical resistance, while presenting high availability, easy transportation, and low cost.\|SUMMARY\|[0006] The following presents a simplified summary to provide a basic understanding of some aspects of the disclosed subject matter. This summary is not an extensive overview. It is not intended to identify key/critical elements or to delineate the scope of the claimed subject matter. Its sole purpose is to present some concepts in a simplified form as a prelude to the more detailed description presented later.\|[0007] According to one aspect, a synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further includes a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|[0008] According to another aspect, infill for a synthetic turf system includes carbon sequestration sand. The carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh. The synthetic turf system may also includes organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|[0009] According to another aspect, a method of preparing a synthetic turf system includes dispersing carbon sequestration sand over a top portion of turf fibers, where the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a bicarbonate or carbonate with rainwater traveling through infill.\|[0010] In other aspects, a carbon sequestration sand-based infill employs a shock pad to achieve a desired and/or proper shock absorption on the turf. The carbon sequestration sand-based infill is most often installed over a layer of permeable backing, where the carbon sequestration sand acts as a stabilizing infill or as part of a stabilizing infill layer. As a stabilizing infill, the carbon sequestration sand performs as a ballast layer that weighs down the turf carpets and mitigates movement.\|[0011] In other aspects, an infill composition for artificial turf fields includes at least one layer of carbon sequestration sand. The carbon sequestration sand includes a particle size distribution of carbon sequestration sand with a size of approximately #4 mesh to #270 mesh. The infill can be installed according to a method of spreading a layer of carbon sequestration sand over a carpet that is on a base of compacted stone. The layers of the carbon sequestration sand are brushed and de-compacted such that the carbon sequestration sand is evenly distributed over the carpet of the turf system.\|[0012] In other aspects, a carbon sequestration sand-based layer may be positioned immediately below the shock pad (if used), on top of the substrate material, e.g., a rock layer. In such a position, the carbon sequestration sand-based layer may have a thickness of 1/16″ to ¼″, with a mesh size in the range of #4 to #270.\|[0013] In still other aspects, carbon sequestration sand may be blended into a stone base layer positioned immediately below the shock pad (if so equipped). In some embodiments, the carbon sequestration sand may be blended into a first of two topping stone base layer system. In other embodiments, the carbon sequestration sand may be blended into some or all of a stone base layer system.\|[0014] In yet another aspect, a layer of carbon sequestration sand may be positioned on a geotextile or subgrade layer. In such a position, the carbon sequestration sand-based layer may have a thickness of 1/16″ to ¼″, with a mesh size in the range of about #4 to #270.\|[0015] In still yet another aspect, carbon sequestration sand may be tilled or blended into native subgrade material. In such a position, the carbon sequestration sand may be blended within the subgrade, e.g., soil, as discussed below.\|[0016] In each of the foregoing aspects, certain carbon sequestration processes can occur as rainwater interacts with the carbon sequestration sand, regardless of the position in the artificial turf system. Further discussion of the processes referenced above are included in the following description.\|[0017] The innovation described herein introduces a carbon sequestration sand-based infill material designed to enhance the mechanical performance or environmental sustainability of synthetic turf systems. The infill material offers ease of application across various layers of the turf system and provides stabilization of the turf fibers while supporting upright positioning. When dispersed over the turf system as a top dressing or integrated within infill layers, the carbon sequestration sand performs as a ballast that mitigates infill migration and enhances field durability. Additionally, the material facilitates carbon capture through chemical reactions with rainwater, enabling the formation of bicarbonates or carbonates that contribute to carbon sequestration while maintaining desired surface properties such as traction, softness, and shock absorption.\|[0018] To the accomplishment of the foregoing and related ends, certain illustrative aspects of the claimed subject matter are described herein in connection with the following description and the annexed drawings. These aspects indicate various ways in which the subject matter may be practiced, all of which are intended to be within the scope of the disclosed subject matter. Other advantages and novel features may become apparent from the following detailed description when considered in conjunction with the drawings.\|[0019] These and other systems, methods, objects, features, and advantages of the present disclosure will be apparent to those skilled in the art from the following detailed description of the preferred embodiment and the drawings.\|[0020] All documents mentioned herein are hereby incorporated in their entirety by reference. References to items in the singular should be understood to include items in the plural, and vice versa, unless explicitly stated otherwise or clear from the text. Grammatical conjunctions are intended to express any and all disjunctive and conjunctive combinations of conjoined clauses, sentences, words, and the like, unless otherwise stated or clear from the context.\|(US20250297409)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0021] FIG. 1 is a partial perspective view of an example synthetic turf system having an infill made of carbon sequestration sand in accordance with some embodiments of the present disclosure.\|[0022] FIG. 2 is a perspective view of an example application system employed in dispersing the carbon sequestration sand over the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0023] FIG. 3 is a perspective view of an example brush employed in grooming the sand into the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0024] FIG. 4 is a partial perspective view of the synthetic turf system of FIG. 1, where an infill made of the carbon sequestration sand in accordance with some embodiments of the present disclosure.\|[0025] FIG. 5 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand layered below a backing in accordance with some embodiments of the present disclosure.\|[0026] FIG. 6 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is blended into a base stone layer in accordance with some embodiments.\|[0027] FIG. 7 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is layered on a geotextile in accordance with some embodiments.\|[0028] FIG. 8 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is diffused into a subgrade in accordance with some embodiments.\|[0029] FIG. 9 is an example process flow for preparing the synthetic turf system of FIG. 1.\|(US20250297409)\|DETAILED DESCRIPTION\|[0030] Various aspects of the subject disclosure are now described in more detail with reference to the annexed drawings, wherein like numerals generally refer to like or corresponding elements throughout. It should be understood, however, that the drawings and detailed description relating thereto are not intended to limit the claimed subject matter to the particular form disclosed. Instead, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the described and claimed subject matter.\|[0031] The following disclosure provides many different embodiments, or examples, for implementing different features of the provided subject matter. Specific examples of components and arrangements are described below to simplify the present disclosure. These are, of course, merely examples and are not intended to be limiting. For example, the formation of a first feature over or on a second feature in the description that follows may include embodiments in which the first and second features are formed in direct contact, and may also include embodiments in which additional features may be formed between the first and second features, such that the first and second features may not be in direct contact. In addition, the present disclosure may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.\|[0032] Further, spatially relative terms, such as “beneath,” “below,” “lower,” “above,” “upper” and the like, may be used herein for ease of description to describe one element or feature's relationship to another element(s) or feature(s) as illustrated in the figures. The spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. The apparatus may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein may likewise be interpreted accordingly.\|[0033] Numerical values in the specification and claims of this application should be understood to include numerical values which are the same when reduced to the same number of significant figures and numerical values which differ from the stated value by less than the experimental error of conventional measurement technique of the type described in the present application to determine the value. All ranges disclosed herein are inclusive of the recited endpoint.\|[0034] The term “about” can be used to include any numerical value that can vary without changing the basic function of that value. When used with a range, “about” also discloses the range defined by the absolute values of the two endpoints, e.g., “about 2 to about 4” also discloses the range “from 2 to 4.” The term “about” may refer to plus or minus 10% of the indicated number.\|[0035] In accordance with varying embodiments discussed herein, there is provided an artificial turf system that utilizes a material derived from one or more types of carbon sequestration sands, including, for example and without limitation, wollastonite sand (general formula CaSiO3), limestone, basalt, or the like. More specifically, the carbon sequestration sands may be formed from silicate rock, ultramafic rock, or reactive rock, and specifically include, for example, wollastonite, basalt, peridotite, olivine, dunite, limestone, and dolostone.\|[0036] In some embodiments, the carbon sequestration sand may be used as an infill material, an intervening layer of material between existing layers of the system, mixed within a particular layer, on or mixed within a substrate, or combinations thereof.\|[0037] In addition to its excellent performance on the field, this carbon sequestration sand also exhibits behaviors that provide for carbon sequestration. Specifically, the material, when in contact with rainwater, causes a chemical reaction to occur between carbonic acid naturally present in the rainwater and the sand, e.g., olivine, wollastonite, etc. The reaction weathers the olivine, wollastonite, etc., and converts the carbonic acid into bicarbonate or carbonate. In this regard, carbonate and bicarbonate tend to be in equilibrium in aqueous solutions caused by weathering reactions because the dissolution of carbon dioxide and minerals generates a dynamic balance governed by pH-dependent acid-base reactions.\|[0038] By converting the carbon dioxide into other substances, the carbon dioxide can no longer be released into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These bicarbonate or carbonate solutions are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments, as well as integrated into marine animal carbonaceous mineral materials. These carbonate sediments form a sink for carbon dioxide.\|[0039] An example implementation of the embodiment described above is shown in FIG. 1. In this regard, FIG. 1 depicts a portion of a synthetic turf system 100 including carbon sequestration sand 102 that may be olivine-based, wollastonite-based, etc. and is utilized in one or more layers of infill materials. In accordance with some embodiments, the carbon sequestration sand 102 may be deposited in a layer having a thickness of about 1/16 to about ¼ inches, and have a particle size of about #4 mesh to about #270 mesh in the U.S. Standard Sieve Series. As will be appreciated, mesh may be defined as the number of openings in one square inch of a screen. A large mesh number means the pores in the screen are small. Sand's mesh size is determined by graining, and the numbers refer to the maximum and minimum grain diameters. 40/80 sand means that 90 percent of the sand by volume is small enough to pass through a #40 mesh screen, but too large to pass through an #80 mesh screen. As such, the range of particle size of the carbon sequestration sand 102 referenced in FIG. 1 may be about #4 mesh (4,750 μm) to about #270 mesh (53 μm).\|[0040] As shown in FIG. 1, the portion of the synthetic turf system 100 includes one or more infill layers 104 (described below), a permeable (e.g., carpet) backing 110, and turf fibers 112 that are artificial grass blades extended substantially perpendicular to the backing 110. With this construction, when the backing 110 is extended flatly in a horizontal direction, such as a stone base layer described in greater detail below, the turf fibers 112 may extend upward in a vertical direction perpendicular to the horizontal direction. While, as depicted, the turf fibers 112 are artificial grass blades, the turf fibers 112 may additionally or alternatively include natural grass blades extended upward from the backing 110, through the carbon sequestration sand 102 and the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0041] The infill layers 104 are positioned above the backing 110, in between the turf fibers 112, and below a top portion 114 of the turf fibers 112. More specifically, the infill layers 104 are disposed directly on top of the backing 110, where the top portion 114 of the turf fibers 112 extends above the infill layers 104. While, as depicted, the example embodiment of FIG. 1 includes multiple layers of infill materials respectively shown as a first layer 120, a second layer 122, and a third layer 124, the synthetic turf system 100 may include more or fewer distinct infill layers. Also, while, as depicted, the carbon sequestration sand 102 is disposed below the third layer 124 and directly contacts the backing 110, where the carbon sequestration sand 102 is interposed between and separates the infill layers 104 from the backing 110, the carbon sequestration sand 102 may additionally or alternatively be incorporated into the first layer 120, the second layer 122, or the third layer 124, or be applied over the third layer 124 as a top dressing of the synthetic turf system 100 without departing from the scope of the present disclosure.\|[0042] In this regard, the carbon sequestration sand 102 may partially or entirely form the first layer 120, the second layer 122, or the third layer 124 with a variety of compositional ranges. In an embodiment, the carbon sequestration sand 102 forms up to 90 percent of the first layer 120, the second layer 122, or the third layer 124 by volume. In a further embodiment, the carbon sequestration sand 102 forms up to 10 percent of the first layer 120, the second layer 122, or the third layer 124 by volume. With this construction, water insoluble components of the first layer 120, the second layer 122, or the third layer 124 reduce an overall wear rate of the synthetic turf system 100, and maintain a minimum volume in the synthetic turf system 100. In this manner, a wear rate and minimum volume of the first layer 120, the second layer 122, or the third layer 124 may be adjusted as desired by adjusting the compositional range of the carbon sequestration sand 102. In an embodiment, the carbon sequestration sand 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0043] The weathering rate and shape of particles forming the carbon sequestration sand 102 are influenced by material selection and particle size distribution. In this regard, consistent particle sizing promotes uniform weathering rates across the one or more infill layers 104, maintaining overall field performance and carbon sequestration efficiency in the synthetic turf system 100. The carbon sequestration sand 102 is accessible to rainwater traveling downward by gravity from the top portion 114 of the turf fibers 112 toward the backing 110. As the carbon sequestration sand 102 weathers through exposure to rainwater, its constituent particles may substantially change morphology, or alternatively may remain largely the same shape. In embodiments, the selected silicate rock, ultramafic rock, or reactive rock materials form weathered particles that maintain a sphericity of about 0.65 to about 0.85. This sphericity range supports stable packing within the synthetic turf system, reduces compaction variability, and ensures continued mechanical performance while facilitating consistent chemical reactions for carbon capture.\|[0044] In an embodiment where the carbon sequestration sand 102 is incorporated in the synthetic turf system 100 as a top dressing, the carbon sequestration sand 102 is periodically dispersed over the top portion 114 of the turf fibers 112 with an application system 130 depicted in FIG. 2. With continued reference to FIG. 2, the application system 130 includes a seed tender 132 and a tractor 134 that disperses the carbon sequestration sand 102 over the synthetic turf system 100 from a broadcaster tool 140. The seed tender 132 is employed in conjunction with a hydraulically-controlled conveyor 142 and a hopper gate 144, which supply the tractor 134 the carbon sequestration sand 102. As the tractor 134 moves at a consistent speed across the synthetic turf system 100 following a predetermined pattern, the hydraulically-controlled conveyor 142 and the hopper gate 144 precisely control a flow rate of the carbon sequestration sand 102 to the tractor 134, ensuring uniform distribution across the synthetic turf system 100.\|[0045] While, as depicted, the application system 130 includes the broadcaster tool 140 pulled by the tractor 134, and continuously fed the carbon sequestration sand 102 by the seed tender 132 along or across the synthetic turf system 100, the application system 130 may additionally or alternatively include a variety of components configured to spread granular material across a field, such as, for example, a self-propelled, manually powered, or power take-off (PTO) driven broadcast material spreader, a pneumatic spreader, an air boom spreader, a drop spreader, a handheld spreader, or an aerial spreader for dispersing the carbon sequestration sand 102 without departing from the scope of the present disclosure.\|[0046] Once the carbon sequestration sand 102 is dispersed across the synthetic turf system 100 by the application system 130, the carbon sequestration sand 102 is brushed into the one or more infill layers 104, including the first layer 120, the second layer 122, and the third layer 124. In this regard, a brush 150 depicted in FIG. 3 grooms the carbon sequestration sand 102 into the one or more infill layers 104. Rotary brush action on the synthetic turf system 100 from the top portion 114 by the brush 150 effectively works the carbon sequestration sand 102 downward between the turf fibers 112, ensuring proper placement within the infill material forming the one or more infill layers 104, while maintaining structural integrity and performance characteristics of the synthetic turf system 100, including at the top portion 114 and the first layer 120.\|[0047] While, as depicted, the brush 150 is a motorized, walk-behind rotary brush apparatus, such as a Shindaiwa or Laymor brush system, the brush 150 may additionally or alternatively include various components for incorporating the carbon sequestration sand 102 into the one or more infill layers 104 such as, for example, a ride-on turf groomer, a tractor-mounted brush that is dragged or PTO driven, or manual turf brushing equipment. Furthermore, brushes employed in such configurations may embody various shapes, sizes, and types, such as, for example, straight brushes, triangular brushes, hydraulic brushes, oscillating brushes, rigid brushes, flexible brushes, or brush assemblies including at least one plurality of brushes. Furthermore, the brush 150 may additionally or alternatively include specialty turf equipment, such as a vacuum or other devices complementary to the brush 150, and utilized to integrate the carbon sequestration sand 102 into the existing infill material of the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0048] Referring back to FIG. 1, infill is representative of material that is deposited over the backing 110 and forms the one or more infill layers 104 around the turf fibers 112. Infill is interspersed between the turf fibers 112 rising out of the backing 110. Infill generally has a depth that covers a portion of the turf fibers 112 (unexposed portion of the artificial fibers/blades) leaving part of the turf fibers 112, i.e., the top portion 114 extending above the infill (exposed portion of the artificial fibers/blades).\|[0049] In accordance with some embodiments, the one or more infill layers 104 assists in supporting the turf fibers 112 in an upright position and is used to provide traction and shock absorption. As a general matter, various types of infill arrangements are contemplated. For example, two layer, three layers, or other arrangements are contemplated. For convenience, the present description primarily discusses two and three layer embodiments.\|[0050] In some embodiments, the first layer 120 may include, for example and without limitation, heartwood or sapwood portions of hardwood or softwood, such as bamboo, cypress, poplar, pine, and cedar. The first layer 120 may additionally or alternatively include, for example and without limitation, cork, corn cobs, olive pits, barks, coconut peat or other organic materials, as well as styrene-butadiene rubber (SBR) particles ethylene propylene diene monomer (EPDM) rubber, other thermoplastics such as polyethylene, polypropylene, or composite materials can be used that combine thermoplastics, elastomers, reinforcements and/or fillers or other sufficient material. In accordance with some embodiments, the second layer 122 of infill material depicted in FIG. 1 may include a mixture of materials, e.g., material of the first layer 120 and a sand material. In such embodiments, the third layer 124 of infill material may include the aforementioned sand material, such that the fourth or lowermost layer is that of the carbon sequestration sand 102.\|[0051] In accordance with some embodiments, a shock pad (not shown) may be employed to achieve a desired shock absorption in accordance with a particular installation/purpose. For example, a shock pad (not shown) may be positioned below the one or more infill layers 104 shown in FIG. 1. As such, the material of the infill layers 104 conveys many of the mechanical properties that may be desired for use as artificial turf infill.\|[0052] In some embodiments, the carbon sequestration sand 102 can be used in combination with the backing 110, and/or a stabilizing infill layer (e.g., sand) 104 to make up the synthetic turf system 100. The synthetic turf system 100, using the described infill material, exhibits superior mechanical performance, a greater mechanical durability, easy availability and mitigates or otherwise avoids issues of floating away when subjected to large amounts of water.\|[0053] In some other embodiments, the backing 110 may be positioned below the carbon sequestration sand 102 shown in FIG. 1. In such embodiments, the backing 110 may correspond to the material into which the turf fibers 112 are woven, held, inserted, etc. Accordingly, the carbon sequestration sand 102 is positioned directly on the backing 110, thereby functioning as a ballast layer. The backing 110 is water permeable, without punched holes, such that the carbon sequestration sand 102 may remain in place at the backing 110, underlying the remainder of the infill layers 104, thereby maximizing contact with rainwater while preventing the carbon sequestration sand 102 from being flushed out of the synthetic turf system 100 via regular drainage measures. More specifically, the backing 110 has a porosity that filters rainwater from the carbon sequestration sand 102 and the one or more infill layers 104 as the rainwater travels downward through the synthetic turf system 100 from the one or more infill layers 104 to below the backing 110.\|[0054] Turning now to FIG. 4, there is shown a more detailed three-dimensional cross-sectional view of a portion of the synthetic turf system 100 utilizing the carbon sequestration sand 102 as a ballast infill material in accordance with the embodiment set forth above in FIG. 1. It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|[0055] As shown in FIG. 4, the synthetic turf system 100, in addition to including the turf fibers 112, the carbon sequestration sand 102, the infill layers 104, and the backing 110, further includes a first base stone layer 200 disposed below the backing 110 and above a second base stone layer 202. The synthetic turf system 100 further includes a geotextile component 204 that is a fabric disposed between the second base stone layer 202 and a subgrade 210. The synthetic turf system 100 may further include a subdrain trench component 212 formed in the subgrade and housing a drainage pipe 214.\|[0056] As discussed above, the carbon sequestration sand 102 may be implemented, for example and without limitation, olivine, wollastonite, basalt, limestone, etc. In operation, with reference to FIGS. 1 and 4, as rainwater contacts the carbon sequestration sand 102, a chemical reaction occurs between carbonic acid naturally present in the rainwater and the sequestration sand. The reaction weathers the carbon sequestration sand 102, e.g., olivine, wollastonite, etc., and converts the carbonic acid into carbonate or bicarbonate. As stated above, the conversion of the carbon dioxide into other substances prevents the release of the carbon dioxide into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. Carbonate and bicarbonate solutions may permeate the first base stone layer 200 and the second base stone layer 202, through the geotextile component 204 and into the subdrain trench component 212 and drainage pipe 214. Thereafter, the carbonate and bicarbonate solutions are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments, forming a sink for carbon dioxide.\|[0057] Turning now to FIG. 5, there is shown another embodiment of the synthetic turf system 100 utilizing the carbon sequestration sand 102. As illustrated in FIG. 5, the carbon sequestration sand 102 is applied on a top surface of the first base stone layer 200, below the backing 110. Application may be made via a suitable top-dressing machine, such as the application system 130 depicted in FIG. 2. In the embodiment of FIG. 5, the carbon sequestration sand 102 may be deposited with a thickness in the range of about 1/16″ to ¼″. The carbon sequestration sand 102 of FIG. 5 may be implemented with a particle size of about #4 mesh to #270 mesh. In such an embodiment, rainwater would flow directly through the one or more infill layers 104, the backing 110, and the carbon sequestration sand 102 and into the first base stone layer 200. Reaction with the rainwater would occur as described above with respect to FIGS. 1 and 4.\|[0058] With reference now to FIG. 6, there is illustrated the synthetic turf system 100 utilizing particles of the carbon sequestration sand 102 in accordance with another embodiment. In the embodiment depicted in FIG. 6, particles of the carbon sequestration sand 102 are incorporated into the first base stone layer 200. In accordance with one non-limiting example, the first base stone layer 200 may be implemented as a layer of stone having a thickness in the range of about 1 inch to about 6 inches, and in some particular embodiments, in the range of about 1 inch to about 2 inches. In such embodiments, the first base stone layer 200 may include for example and without limitation, a suitable drainage stone, such as gravel (e.g., granite) or the like. The carbon sequestration sand 102 may be suitably mixed with the stone to distribute the carbon sequestration sand 102 throughout the first base stone layer 200. In some embodiments, a single, e.g., uniform, base stone layer (not shown) may be utilized. In such embodiments, the carbon sequestration sand 102 may be blended into the single base stone layer, e.g., to a certain depth thereof (e.g., the top 1″ or 2″ thereof), or throughout the base stone layer. As described in greater detail above, reaction of the carbon sequestration sand 102 with rainwater would occur as described above with respect to FIGS. 1, 4, and 5.\|[0059] Turning now to FIG. 7, there is shown another embodiment of the synthetic turf system 100 utilizing carbon sequestration sand 102. As illustrated in FIG. 7, the carbon sequestration sand 102 may be on the geotextile component 204. In such a position, the carbon sequestration sand 102 may form a layer having a thickness of about 1/16″ to about ¼″, with a mesh size in the range of about #4 to about #270. Stated another way, the layer of carbon sequestration sand 102 may be applied at a bottom of the second base stone layer 202, as shown in FIG. 7. In accordance with one non-limiting example, the second base stone layer 202 may be implemented as a layer of stone having a thickness in the range of about 2 inches to about 6 inches, and in some particular embodiments, in the range of about 3 inches to about 4 inches. In such embodiments, the second base stone layer 202 may include, for example and without limitation, a suitable drainage stone, such as gravel (e.g., granite) or the like.\|[0060] In an embodiment, the first base stone layer 200 or the second base stone layer 202 includes silicate rocks, ultramafic rocks, or otherwise reactive rocks such as, for example, basalt, peridotite, olivine, dunite, limestone, and dolostone. Notably, in such an embodiment, the first base stone layer 200 or the second base stone layer 202 may perform carbon sequestration upon weathering by rainwater, in addition to the carbon sequestration sand 102, increasing an overall carbon sequestration capacity of the synthetic turf system 100.\|[0061] Although not shown, it is contemplated that the carbon sequestration sand 102 may be blended with the stone of the second base stone layer 202 similar to the manner described above with respect to FIG. 6. Similarly, although not illustrated in the accompanying figures, it is further contemplated that the carbon sequestration sand 102 may be blended with the stone of the subdrain trench component 212, or layered in the subdrain trench component 212 without blending. The above described positions of the carbon sequestration sand 102 would also enable the carbon capture reaction described above with respect to FIGS. 1 and 4-6.\|[0062] Referring now to FIG. 8, there is shown the synthetic turf system 100 utilizing the carbon sequestration sand 102 in accordance with another embodiment. As illustrated in FIG. 8, the carbon sequestration sand 102 may be tilled and incorporated into the subgrade 210 of the synthetic turf system 100, e.g., soil, sediment, etc. In such an implementation, the geotextile component 204 layered over the subgrade 210, and a 6″ to 8″ combined thickness of the first base stone layer 200 and the second base stone layer 202 may be installed on the subgrade 210 with the carbon sequestration sand 102 distributed therein. It will be appreciated that more carbon sequestration sand 102 may be used with this embodiment than the embodiments described above, thereby providing the synthetic turf system 100 additional carbon sequestration capability.\|[0063] Furthermore, it will be appreciated that by placing the carbon sequestration sand 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air. That is, as organic matter breaks down it creates additional carbon dioxide. As such, having the carbon sequestration sand 102 in the subgrade 210 where there is potential for more water availability increases the ability for the weathering reaction to occur, thereby facilitating carbon sequestration. In addition, as described above with respect to FIGS. 1 and 4-7, rainwater reaction with the carbon sequestration sand 102 provides the aforementioned carbon capture benefits.\|[0064] Referring to FIG. 9, a method 300 for preparing a synthetic turf system will be described according to an exemplary embodiment. FIG. 9 will be described with reference to FIGS. 1-8. For simplicity, the method 300 will be described as a sequence of blocks, but the elements of the method 300 can be organized into different architectures, elements, stages, and/or processes.\|[0065] At block 302, the method 300 includes measuring an aspect of the synthetic turf system 100. More specifically, a user may measure a thickness of an infill layer, such as one of the infill layers 104, may measure an acidity of rainwater at the infill layer, and may measure a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer.\|[0066] At block 304, the method 300 includes preblending or layering the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112. In an embodiment, the method 300 includes determining desired compositional ranges of the carbon sequestration sand 102 based on the measurement or measurements taken at block 302. In this manner, the wear rate and the minimum volume of the one or more infill layers 104 is controlled by adjusting the compositional ranges of components of the carbon sequestration sand 102. In an embodiment, the carbon sequestration sand 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0067] At block 310, the method 300 includes dispersing the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112, where the carbon sequestration sand 102 includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through the one or more infill layers 104 by gravity. In an embodiment, dispersing the carbon sequestration sand 102 includes dispersing a predetermined quantity of the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112 as a top dressing based on the measurement taken at block 302.\|[0068] At block 312, the method 300 includes grooming the carbon sequestration sand 102 into the one or more infill layers 104 of the synthetic turf system 100, between the turf fibers 112, at the backing 110 of the synthetic turf system 100. In this regard, the brush 150 grooms the carbon sequestration sand 102 into and through the one or more infill layers 104, where the carbon sequestration sand 102 contacts and rests on the backing 110.\|[0069] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions and/or alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc., do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.\|[0070] While specific embodiments are shown and described herein, it is contemplated that alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc. without departing from the spirit and/or scope of the innovation as described in detail. These alternative embodiments are to be included within the spirit and scope of the innovation as described and claimed herein.\|[0071] Although the subject matter has been described in language specific to structural features or methodological acts, it is to be understood that the subject matter of the appended claims is not necessarily limited to the specific features or acts described above. Rather, the specific features and acts described above are disclosed as example aspects.\|[0072] Various operations of aspects are provided herein. The order in which one or more or all of the operations are described should not be construed as to imply that these operations are necessarily order dependent. Alternative ordering will be appreciated based on this description. Further, not all operations may necessarily be present in each aspect provided herein.\|[0073] As used in this application, “or” is intended to mean an inclusive “or” rather than an exclusive “or”. Further, an inclusive “or” may include any combination thereof (e.g., A, B, or any combination thereof). In addition, “a” and “an” as used in this application are generally construed to mean “one or more” unless specified otherwise or clear from context to be directed to a singular form. Additionally, at least one of A and B and/or the like generally means A or B or both A and B. Further, to the extent that “includes”, “having”, “has”, “with”, or variants thereof are used in either the detailed description or the claims, such terms are intended to be inclusive in a manner similar to the term “comprising”.\|[0074] Further, unless specified otherwise, “first”, “second”, or the like are not intended to imply a temporal aspect, a spatial aspect, an ordering, etc. Rather, such terms are merely used as identifiers, names, etc. for features, elements, items, etc. For example, a first channel and a second channel generally correspond to channel A and channel B or two different or two identical channels or the same channel. Additionally, “comprising”, “comprises”, “including”, “includes”, or the like generally means comprising or including, but not limited thereto.\|[0075] Further, the term “in” as used to describe an object with respect to a given direction (e.g., an edge extended in a left-right direction) is intended to denote an orientation that is substantially parallel to the specified direction. In contrast, the term “along” as used to describe an object with respect to a given direction (e.g., an edge extended along a vertical direction) is intended to indicate that a feature or element possesses a common vector component in that direction, even if its overall alignment is not strictly parallel.\|[0076] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.	(US20250297409)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] The application claims priority to and the benefit of U.S. Provisional Patent Application No. 63/569,558, filed on Mar. 25, 2024, entitled “Carbon Capture System and Method for Synthetic Turf Fields”, which we incorporate by reference in its entirety.\|(US20250297409)\|BACKGROUND\|[0002] Artificial or synthetic turf fields are composed of three primary components—from bottom to top: shock pad, carpet, and infill. These components are generally assembled on top of a base of compacted stone. The shock pad is optional and serves to convey much of the shock absorption performance of the turf field, required for the safety of those playing on the surface in the case of impact with the surface. The carpet serves to mimic the blades of grass and root zone, conveying the softness and traction of the surface as well as many of the ball interaction properties. The infill is generally constituted of at least two layers, the bottom layer of which serves to weight down and stabilize the carpets that it is laid onto, whereas the top layers serve as an additional interface layer to those playing on the field, conveying surface softness, friction, traction, and much of the mechanical properties of the field that are felt directly by the players.\|[0003] As a matter of background, a significant amount of engineering and development is devoted to developing artificial turf field systems. With respect to the infill, each kind of material has its own performance and structural characteristics. Obtaining the right composition and arrangement of materials can be challenging.\|[0004] Furthermore, when installation of a synthetic turf field occurs, generally speaking, a living, natural turf field is being replaced with an artificial one. In this process, a living organism, e.g., grass, plants, etc., which naturally removes carbon dioxide from the atmosphere is removed. Additionally, the construction associated with a synthetic turf field, as well as the actual manufacturing of the synthetic turf, result in additional carbon entering the atmosphere.\|[0005] As such, there remains a need for environmentally friendly and ultimately carbon-neutral or carbon-offsetting infill materials that present good mechanical properties and mechanical resistance, while presenting high availability, easy transportation, and low cost.\|SUMMARY\|[0006] The following presents a simplified summary to provide a basic understanding of some aspects of the disclosed subject matter. This summary is not an extensive overview. It is not intended to identify key/critical elements or to delineate the scope of the claimed subject matter. Its sole purpose is to present some concepts in a simplified form as a prelude to the more detailed description presented later.\|[0007] According to one aspect, a synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further includes a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|[0008] According to another aspect, infill for a synthetic turf system includes carbon sequestration sand. The carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh. The synthetic turf system may also includes organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|[0009] According to another aspect, a method of preparing a synthetic turf system includes dispersing carbon sequestration sand over a top portion of turf fibers, where the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a bicarbonate or carbonate with rainwater traveling through infill.\|[0010] In other aspects, a carbon sequestration sand-based infill employs a shock pad to achieve a desired and/or proper shock absorption on the turf. The carbon sequestration sand-based infill is most often installed over a layer of permeable backing, where the carbon sequestration sand acts as a stabilizing infill or as part of a stabilizing infill layer. As a stabilizing infill, the carbon sequestration sand performs as a ballast layer that weighs down the turf carpets and mitigates movement.\|[0011] In other aspects, an infill composition for artificial turf fields includes at least one layer of carbon sequestration sand. The carbon sequestration sand includes a particle size distribution of carbon sequestration sand with a size of approximately #4 mesh to #270 mesh. The infill can be installed according to a method of spreading a layer of carbon sequestration sand over a carpet that is on a base of compacted stone. The layers of the carbon sequestration sand are brushed and de-compacted such that the carbon sequestration sand is evenly distributed over the carpet of the turf system.\|[0012] In other aspects, a carbon sequestration sand-based layer may be positioned immediately below the shock pad (if used), on top of the substrate material, e.g., a rock layer. In such a position, the carbon sequestration sand-based layer may have a thickness of 1/16″ to ¼″, with a mesh size in the range of #4 to #270.\|[0013] In still other aspects, carbon sequestration sand may be blended into a stone base layer positioned immediately below the shock pad (if so equipped). In some embodiments, the carbon sequestration sand may be blended into a first of two topping stone base layer system. In other embodiments, the carbon sequestration sand may be blended into some or all of a stone base layer system.\|[0014] In yet another aspect, a layer of carbon sequestration sand may be positioned on a geotextile or subgrade layer. In such a position, the carbon sequestration sand-based layer may have a thickness of 1/16″ to ¼″, with a mesh size in the range of about #4 to #270.\|[0015] In still yet another aspect, carbon sequestration sand may be tilled or blended into native subgrade material. In such a position, the carbon sequestration sand may be blended within the subgrade, e.g., soil, as discussed below.\|[0016] In each of the foregoing aspects, certain carbon sequestration processes can occur as rainwater interacts with the carbon sequestration sand, regardless of the position in the artificial turf system. Further discussion of the processes referenced above are included in the following description.\|[0017] The innovation described herein introduces a carbon sequestration sand-based infill material designed to enhance the mechanical performance or environmental sustainability of synthetic turf systems. The infill material offers ease of application across various layers of the turf system and provides stabilization of the turf fibers while supporting upright positioning. When dispersed over the turf system as a top dressing or integrated within infill layers, the carbon sequestration sand performs as a ballast that mitigates infill migration and enhances field durability. Additionally, the material facilitates carbon capture through chemical reactions with rainwater, enabling the formation of bicarbonates or carbonates that contribute to carbon sequestration while maintaining desired surface properties such as traction, softness, and shock absorption.\|[0018] To the accomplishment of the foregoing and related ends, certain illustrative aspects of the claimed subject matter are described herein in connection with the following description and the annexed drawings. These aspects indicate various ways in which the subject matter may be practiced, all of which are intended to be within the scope of the disclosed subject matter. Other advantages and novel features may become apparent from the following detailed description when considered in conjunction with the drawings.\|[0019] These and other systems, methods, objects, features, and advantages of the present disclosure will be apparent to those skilled in the art from the following detailed description of the preferred embodiment and the drawings.\|[0020] All documents mentioned herein are hereby incorporated in their entirety by reference. References to items in the singular should be understood to include items in the plural, and vice versa, unless explicitly stated otherwise or clear from the text. Grammatical conjunctions are intended to express any and all disjunctive and conjunctive combinations of conjoined clauses, sentences, words, and the like, unless otherwise stated or clear from the context.\|(US20250297409)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0021] FIG. 1 is a partial perspective view of an example synthetic turf system having an infill made of carbon sequestration sand in accordance with some embodiments of the present disclosure.\|[0022] FIG. 2 is a perspective view of an example application system employed in dispersing the carbon sequestration sand over the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0023] FIG. 3 is a perspective view of an example brush employed in grooming the sand into the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0024] FIG. 4 is a partial perspective view of the synthetic turf system of FIG. 1, where an infill made of the carbon sequestration sand in accordance with some embodiments of the present disclosure.\|[0025] FIG. 5 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand layered below a backing in accordance with some embodiments of the present disclosure.\|[0026] FIG. 6 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is blended into a base stone layer in accordance with some embodiments.\|[0027] FIG. 7 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is layered on a geotextile in accordance with some embodiments.\|[0028] FIG. 8 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is diffused into a subgrade in accordance with some embodiments.\|[0029] FIG. 9 is an example process flow for preparing the synthetic turf system of FIG. 1.\|(US20250297409)\|DETAILED DESCRIPTION\|[0030] Various aspects of the subject disclosure are now described in more detail with reference to the annexed drawings, wherein like numerals generally refer to like or corresponding elements throughout. It should be understood, however, that the drawings and detailed description relating thereto are not intended to limit the claimed subject matter to the particular form disclosed. Instead, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the described and claimed subject matter.\|[0031] The following disclosure provides many different embodiments, or examples, for implementing different features of the provided subject matter. Specific examples of components and arrangements are described below to simplify the present disclosure. These are, of course, merely examples and are not intended to be limiting. For example, the formation of a first feature over or on a second feature in the description that follows may include embodiments in which the first and second features are formed in direct contact, and may also include embodiments in which additional features may be formed between the first and second features, such that the first and second features may not be in direct contact. In addition, the present disclosure may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.\|[0032] Further, spatially relative terms, such as “beneath,” “below,” “lower,” “above,” “upper” and the like, may be used herein for ease of description to describe one element or feature's relationship to another element(s) or feature(s) as illustrated in the figures. The spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. The apparatus may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein may likewise be interpreted accordingly.\|[0033] Numerical values in the specification and claims of this application should be understood to include numerical values which are the same when reduced to the same number of significant figures and numerical values which differ from the stated value by less than the experimental error of conventional measurement technique of the type described in the present application to determine the value. All ranges disclosed herein are inclusive of the recited endpoint.\|[0034] The term “about” can be used to include any numerical value that can vary without changing the basic function of that value. When used with a range, “about” also discloses the range defined by the absolute values of the two endpoints, e.g., “about 2 to about 4” also discloses the range “from 2 to 4.” The term “about” may refer to plus or minus 10% of the indicated number.\|[0035] In accordance with varying embodiments discussed herein, there is provided an artificial turf system that utilizes a material derived from one or more types of carbon sequestration sands, including, for example and without limitation, wollastonite sand (general formula CaSiO3), limestone, basalt, or the like. More specifically, the carbon sequestration sands may be formed from silicate rock, ultramafic rock, or reactive rock, and specifically include, for example, wollastonite, basalt, peridotite, olivine, dunite, limestone, and dolostone.\|[0036] In some embodiments, the carbon sequestration sand may be used as an infill material, an intervening layer of material between existing layers of the system, mixed within a particular layer, on or mixed within a substrate, or combinations thereof.\|[0037] In addition to its excellent performance on the field, this carbon sequestration sand also exhibits behaviors that provide for carbon sequestration. Specifically, the material, when in contact with rainwater, causes a chemical reaction to occur between carbonic acid naturally present in the rainwater and the sand, e.g., olivine, wollastonite, etc. The reaction weathers the olivine, wollastonite, etc., and converts the carbonic acid into bicarbonate or carbonate. In this regard, carbonate and bicarbonate tend to be in equilibrium in aqueous solutions caused by weathering reactions because the dissolution of carbon dioxide and minerals generates a dynamic balance governed by pH-dependent acid-base reactions.\|[0038] By converting the carbon dioxide into other substances, the carbon dioxide can no longer be released into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These bicarbonate or carbonate solutions are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments, as well as integrated into marine animal carbonaceous mineral materials. These carbonate sediments form a sink for carbon dioxide.\|[0039] An example implementation of the embodiment described above is shown in FIG. 1. In this regard, FIG. 1 depicts a portion of a synthetic turf system 100 including carbon sequestration sand 102 that may be olivine-based, wollastonite-based, etc. and is utilized in one or more layers of infill materials. In accordance with some embodiments, the carbon sequestration sand 102 may be deposited in a layer having a thickness of about 1/16 to about ¼ inches, and have a particle size of about #4 mesh to about #270 mesh in the U.S. Standard Sieve Series. As will be appreciated, mesh may be defined as the number of openings in one square inch of a screen. A large mesh number means the pores in the screen are small. Sand's mesh size is determined by graining, and the numbers refer to the maximum and minimum grain diameters. 40/80 sand means that 90 percent of the sand by volume is small enough to pass through a #40 mesh screen, but too large to pass through an #80 mesh screen. As such, the range of particle size of the carbon sequestration sand 102 referenced in FIG. 1 may be about #4 mesh (4,750 μm) to about #270 mesh (53 μm).\|[0040] As shown in FIG. 1, the portion of the synthetic turf system 100 includes one or more infill layers 104 (described below), a permeable (e.g., carpet) backing 110, and turf fibers 112 that are artificial grass blades extended substantially perpendicular to the backing 110. With this construction, when the backing 110 is extended flatly in a horizontal direction, such as a stone base layer described in greater detail below, the turf fibers 112 may extend upward in a vertical direction perpendicular to the horizontal direction. While, as depicted, the turf fibers 112 are artificial grass blades, the turf fibers 112 may additionally or alternatively include natural grass blades extended upward from the backing 110, through the carbon sequestration sand 102 and the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0041] The infill layers 104 are positioned above the backing 110, in between the turf fibers 112, and below a top portion 114 of the turf fibers 112. More specifically, the infill layers 104 are disposed directly on top of the backing 110, where the top portion 114 of the turf fibers 112 extends above the infill layers 104. While, as depicted, the example embodiment of FIG. 1 includes multiple layers of infill materials respectively shown as a first layer 120, a second layer 122, and a third layer 124, the synthetic turf system 100 may include more or fewer distinct infill layers. Also, while, as depicted, the carbon sequestration sand 102 is disposed below the third layer 124 and directly contacts the backing 110, where the carbon sequestration sand 102 is interposed between and separates the infill layers 104 from the backing 110, the carbon sequestration sand 102 may additionally or alternatively be incorporated into the first layer 120, the second layer 122, or the third layer 124, or be applied over the third layer 124 as a top dressing of the synthetic turf system 100 without departing from the scope of the present disclosure.\|[0042] In this regard, the carbon sequestration sand 102 may partially or entirely form the first layer 120, the second layer 122, or the third layer 124 with a variety of compositional ranges. In an embodiment, the carbon sequestration sand 102 forms up to 90 percent of the first layer 120, the second layer 122, or the third layer 124 by volume. In a further embodiment, the carbon sequestration sand 102 forms up to 10 percent of the first layer 120, the second layer 122, or the third layer 124 by volume. With this construction, water insoluble components of the first layer 120, the second layer 122, or the third layer 124 reduce an overall wear rate of the synthetic turf system 100, and maintain a minimum volume in the synthetic turf system 100. In this manner, a wear rate and minimum volume of the first layer 120, the second layer 122, or the third layer 124 may be adjusted as desired by adjusting the compositional range of the carbon sequestration sand 102. In an embodiment, the carbon sequestration sand 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0043] The weathering rate and shape of particles forming the carbon sequestration sand 102 are influenced by material selection and particle size distribution. In this regard, consistent particle sizing promotes uniform weathering rates across the one or more infill layers 104, maintaining overall field performance and carbon sequestration efficiency in the synthetic turf system 100. The carbon sequestration sand 102 is accessible to rainwater traveling downward by gravity from the top portion 114 of the turf fibers 112 toward the backing 110. As the carbon sequestration sand 102 weathers through exposure to rainwater, its constituent particles may substantially change morphology, or alternatively may remain largely the same shape. In embodiments, the selected silicate rock, ultramafic rock, or reactive rock materials form weathered particles that maintain a sphericity of about 0.65 to about 0.85. This sphericity range supports stable packing within the synthetic turf system, reduces compaction variability, and ensures continued mechanical performance while facilitating consistent chemical reactions for carbon capture.\|[0044] In an embodiment where the carbon sequestration sand 102 is incorporated in the synthetic turf system 100 as a top dressing, the carbon sequestration sand 102 is periodically dispersed over the top portion 114 of the turf fibers 112 with an application system 130 depicted in FIG. 2. With continued reference to FIG. 2, the application system 130 includes a seed tender 132 and a tractor 134 that disperses the carbon sequestration sand 102 over the synthetic turf system 100 from a broadcaster tool 140. The seed tender 132 is employed in conjunction with a hydraulically-controlled conveyor 142 and a hopper gate 144, which supply the tractor 134 the carbon sequestration sand 102. As the tractor 134 moves at a consistent speed across the synthetic turf system 100 following a predetermined pattern, the hydraulically-controlled conveyor 142 and the hopper gate 144 precisely control a flow rate of the carbon sequestration sand 102 to the tractor 134, ensuring uniform distribution across the synthetic turf system 100.\|[0045] While, as depicted, the application system 130 includes the broadcaster tool 140 pulled by the tractor 134, and continuously fed the carbon sequestration sand 102 by the seed tender 132 along or across the synthetic turf system 100, the application system 130 may additionally or alternatively include a variety of components configured to spread granular material across a field, such as, for example, a self-propelled, manually powered, or power take-off (PTO) driven broadcast material spreader, a pneumatic spreader, an air boom spreader, a drop spreader, a handheld spreader, or an aerial spreader for dispersing the carbon sequestration sand 102 without departing from the scope of the present disclosure.\|[0046] Once the carbon sequestration sand 102 is dispersed across the synthetic turf system 100 by the application system 130, the carbon sequestration sand 102 is brushed into the one or more infill layers 104, including the first layer 120, the second layer 122, and the third layer 124. In this regard, a brush 150 depicted in FIG. 3 grooms the carbon sequestration sand 102 into the one or more infill layers 104. Rotary brush action on the synthetic turf system 100 from the top portion 114 by the brush 150 effectively works the carbon sequestration sand 102 downward between the turf fibers 112, ensuring proper placement within the infill material forming the one or more infill layers 104, while maintaining structural integrity and performance characteristics of the synthetic turf system 100, including at the top portion 114 and the first layer 120.\|[0047] While, as depicted, the brush 150 is a motorized, walk-behind rotary brush apparatus, such as a Shindaiwa or Laymor brush system, the brush 150 may additionally or alternatively include various components for incorporating the carbon sequestration sand 102 into the one or more infill layers 104 such as, for example, a ride-on turf groomer, a tractor-mounted brush that is dragged or PTO driven, or manual turf brushing equipment. Furthermore, brushes employed in such configurations may embody various shapes, sizes, and types, such as, for example, straight brushes, triangular brushes, hydraulic brushes, oscillating brushes, rigid brushes, flexible brushes, or brush assemblies including at least one plurality of brushes. Furthermore, the brush 150 may additionally or alternatively include specialty turf equipment, such as a vacuum or other devices complementary to the brush 150, and utilized to integrate the carbon sequestration sand 102 into the existing infill material of the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0048] Referring back to FIG. 1, infill is representative of material that is deposited over the backing 110 and forms the one or more infill layers 104 around the turf fibers 112. Infill is interspersed between the turf fibers 112 rising out of the backing 110. Infill generally has a depth that covers a portion of the turf fibers 112 (unexposed portion of the artificial fibers/blades) leaving part of the turf fibers 112, i.e., the top portion 114 extending above the infill (exposed portion of the artificial fibers/blades).\|[0049] In accordance with some embodiments, the one or more infill layers 104 assists in supporting the turf fibers 112 in an upright position and is used to provide traction and shock absorption. As a general matter, various types of infill arrangements are contemplated. For example, two layer, three layers, or other arrangements are contemplated. For convenience, the present description primarily discusses two and three layer embodiments.\|[0050] In some embodiments, the first layer 120 may include, for example and without limitation, heartwood or sapwood portions of hardwood or softwood, such as bamboo, cypress, poplar, pine, and cedar. The first layer 120 may additionally or alternatively include, for example and without limitation, cork, corn cobs, olive pits, barks, coconut peat or other organic materials, as well as styrene-butadiene rubber (SBR) particles ethylene propylene diene monomer (EPDM) rubber, other thermoplastics such as polyethylene, polypropylene, or composite materials can be used that combine thermoplastics, elastomers, reinforcements and/or fillers or other sufficient material. In accordance with some embodiments, the second layer 122 of infill material depicted in FIG. 1 may include a mixture of materials, e.g., material of the first layer 120 and a sand material. In such embodiments, the third layer 124 of infill material may include the aforementioned sand material, such that the fourth or lowermost layer is that of the carbon sequestration sand 102.\|[0051] In accordance with some embodiments, a shock pad (not shown) may be employed to achieve a desired shock absorption in accordance with a particular installation/purpose. For example, a shock pad (not shown) may be positioned below the one or more infill layers 104 shown in FIG. 1. As such, the material of the infill layers 104 conveys many of the mechanical properties that may be desired for use as artificial turf infill.\|[0052] In some embodiments, the carbon sequestration sand 102 can be used in combination with the backing 110, and/or a stabilizing infill layer (e.g., sand) 104 to make up the synthetic turf system 100. The synthetic turf system 100, using the described infill material, exhibits superior mechanical performance, a greater mechanical durability, easy availability and mitigates or otherwise avoids issues of floating away when subjected to large amounts of water.\|[0053] In some other embodiments, the backing 110 may be positioned below the carbon sequestration sand 102 shown in FIG. 1. In such embodiments, the backing 110 may correspond to the material into which the turf fibers 112 are woven, held, inserted, etc. Accordingly, the carbon sequestration sand 102 is positioned directly on the backing 110, thereby functioning as a ballast layer. The backing 110 is water permeable, without punched holes, such that the carbon sequestration sand 102 may remain in place at the backing 110, underlying the remainder of the infill layers 104, thereby maximizing contact with rainwater while preventing the carbon sequestration sand 102 from being flushed out of the synthetic turf system 100 via regular drainage measures. More specifically, the backing 110 has a porosity that filters rainwater from the carbon sequestration sand 102 and the one or more infill layers 104 as the rainwater travels downward through the synthetic turf system 100 from the one or more infill layers 104 to below the backing 110.\|[0054] Turning now to FIG. 4, there is shown a more detailed three-dimensional cross-sectional view of a portion of the synthetic turf system 100 utilizing the carbon sequestration sand 102 as a ballast infill material in accordance with the embodiment set forth above in FIG. 1. It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|[0055] As shown in FIG. 4, the synthetic turf system 100, in addition to including the turf fibers 112, the carbon sequestration sand 102, the infill layers 104, and the backing 110, further includes a first base stone layer 200 disposed below the backing 110 and above a second base stone layer 202. The synthetic turf system 100 further includes a geotextile component 204 that is a fabric disposed between the second base stone layer 202 and a subgrade 210. The synthetic turf system 100 may further include a subdrain trench component 212 formed in the subgrade and housing a drainage pipe 214.\|[0056] As discussed above, the carbon sequestration sand 102 may be implemented, for example and without limitation, olivine, wollastonite, basalt, limestone, etc. In operation, with reference to FIGS. 1 and 4, as rainwater contacts the carbon sequestration sand 102, a chemical reaction occurs between carbonic acid naturally present in the rainwater and the sequestration sand. The reaction weathers the carbon sequestration sand 102, e.g., olivine, wollastonite, etc., and converts the carbonic acid into carbonate or bicarbonate. As stated above, the conversion of the carbon dioxide into other substances prevents the release of the carbon dioxide into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. Carbonate and bicarbonate solutions may permeate the first base stone layer 200 and the second base stone layer 202, through the geotextile component 204 and into the subdrain trench component 212 and drainage pipe 214. Thereafter, the carbonate and bicarbonate solutions are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments, forming a sink for carbon dioxide.\|[0057] Turning now to FIG. 5, there is shown another embodiment of the synthetic turf system 100 utilizing the carbon sequestration sand 102. As illustrated in FIG. 5, the carbon sequestration sand 102 is applied on a top surface of the first base stone layer 200, below the backing 110. Application may be made via a suitable top-dressing machine, such as the application system 130 depicted in FIG. 2. In the embodiment of FIG. 5, the carbon sequestration sand 102 may be deposited with a thickness in the range of about 1/16″ to ¼″. The carbon sequestration sand 102 of FIG. 5 may be implemented with a particle size of about #4 mesh to #270 mesh. In such an embodiment, rainwater would flow directly through the one or more infill layers 104, the backing 110, and the carbon sequestration sand 102 and into the first base stone layer 200. Reaction with the rainwater would occur as described above with respect to FIGS. 1 and 4.\|[0058] With reference now to FIG. 6, there is illustrated the synthetic turf system 100 utilizing particles of the carbon sequestration sand 102 in accordance with another embodiment. In the embodiment depicted in FIG. 6, particles of the carbon sequestration sand 102 are incorporated into the first base stone layer 200. In accordance with one non-limiting example, the first base stone layer 200 may be implemented as a layer of stone having a thickness in the range of about 1 inch to about 6 inches, and in some particular embodiments, in the range of about 1 inch to about 2 inches. In such embodiments, the first base stone layer 200 may include for example and without limitation, a suitable drainage stone, such as gravel (e.g., granite) or the like. The carbon sequestration sand 102 may be suitably mixed with the stone to distribute the carbon sequestration sand 102 throughout the first base stone layer 200. In some embodiments, a single, e.g., uniform, base stone layer (not shown) may be utilized. In such embodiments, the carbon sequestration sand 102 may be blended into the single base stone layer, e.g., to a certain depth thereof (e.g., the top 1″ or 2″ thereof), or throughout the base stone layer. As described in greater detail above, reaction of the carbon sequestration sand 102 with rainwater would occur as described above with respect to FIGS. 1, 4, and 5.\|[0059] Turning now to FIG. 7, there is shown another embodiment of the synthetic turf system 100 utilizing carbon sequestration sand 102. As illustrated in FIG. 7, the carbon sequestration sand 102 may be on the geotextile component 204. In such a position, the carbon sequestration sand 102 may form a layer having a thickness of about 1/16″ to about ¼″, with a mesh size in the range of about #4 to about #270. Stated another way, the layer of carbon sequestration sand 102 may be applied at a bottom of the second base stone layer 202, as shown in FIG. 7. In accordance with one non-limiting example, the second base stone layer 202 may be implemented as a layer of stone having a thickness in the range of about 2 inches to about 6 inches, and in some particular embodiments, in the range of about 3 inches to about 4 inches. In such embodiments, the second base stone layer 202 may include, for example and without limitation, a suitable drainage stone, such as gravel (e.g., granite) or the like.\|[0060] In an embodiment, the first base stone layer 200 or the second base stone layer 202 includes silicate rocks, ultramafic rocks, or otherwise reactive rocks such as, for example, basalt, peridotite, olivine, dunite, limestone, and dolostone. Notably, in such an embodiment, the first base stone layer 200 or the second base stone layer 202 may perform carbon sequestration upon weathering by rainwater, in addition to the carbon sequestration sand 102, increasing an overall carbon sequestration capacity of the synthetic turf system 100.\|[0061] Although not shown, it is contemplated that the carbon sequestration sand 102 may be blended with the stone of the second base stone layer 202 similar to the manner described above with respect to FIG. 6. Similarly, although not illustrated in the accompanying figures, it is further contemplated that the carbon sequestration sand 102 may be blended with the stone of the subdrain trench component 212, or layered in the subdrain trench component 212 without blending. The above described positions of the carbon sequestration sand 102 would also enable the carbon capture reaction described above with respect to FIGS. 1 and 4-6.\|[0062] Referring now to FIG. 8, there is shown the synthetic turf system 100 utilizing the carbon sequestration sand 102 in accordance with another embodiment. As illustrated in FIG. 8, the carbon sequestration sand 102 may be tilled and incorporated into the subgrade 210 of the synthetic turf system 100, e.g., soil, sediment, etc. In such an implementation, the geotextile component 204 layered over the subgrade 210, and a 6″ to 8″ combined thickness of the first base stone layer 200 and the second base stone layer 202 may be installed on the subgrade 210 with the carbon sequestration sand 102 distributed therein. It will be appreciated that more carbon sequestration sand 102 may be used with this embodiment than the embodiments described above, thereby providing the synthetic turf system 100 additional carbon sequestration capability.\|[0063] Furthermore, it will be appreciated that by placing the carbon sequestration sand 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air. That is, as organic matter breaks down it creates additional carbon dioxide. As such, having the carbon sequestration sand 102 in the subgrade 210 where there is potential for more water availability increases the ability for the weathering reaction to occur, thereby facilitating carbon sequestration. In addition, as described above with respect to FIGS. 1 and 4-7, rainwater reaction with the carbon sequestration sand 102 provides the aforementioned carbon capture benefits.\|[0064] Referring to FIG. 9, a method 300 for preparing a synthetic turf system will be described according to an exemplary embodiment. FIG. 9 will be described with reference to FIGS. 1-8. For simplicity, the method 300 will be described as a sequence of blocks, but the elements of the method 300 can be organized into different architectures, elements, stages, and/or processes.\|[0065] At block 302, the method 300 includes measuring an aspect of the synthetic turf system 100. More specifically, a user may measure a thickness of an infill layer, such as one of the infill layers 104, may measure an acidity of rainwater at the infill layer, and may measure a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer.\|[0066] At block 304, the method 300 includes preblending or layering the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112. In an embodiment, the method 300 includes determining desired compositional ranges of the carbon sequestration sand 102 based on the measurement or measurements taken at block 302. In this manner, the wear rate and the minimum volume of the one or more infill layers 104 is controlled by adjusting the compositional ranges of components of the carbon sequestration sand 102. In an embodiment, the carbon sequestration sand 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0067] At block 310, the method 300 includes dispersing the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112, where the carbon sequestration sand 102 includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through the one or more infill layers 104 by gravity. In an embodiment, dispersing the carbon sequestration sand 102 includes dispersing a predetermined quantity of the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112 as a top dressing based on the measurement taken at block 302.\|[0068] At block 312, the method 300 includes grooming the carbon sequestration sand 102 into the one or more infill layers 104 of the synthetic turf system 100, between the turf fibers 112, at the backing 110 of the synthetic turf system 100. In this regard, the brush 150 grooms the carbon sequestration sand 102 into and through the one or more infill layers 104, where the carbon sequestration sand 102 contacts and rests on the backing 110.\|[0069] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions and/or alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc., do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.\|[0070] While specific embodiments are shown and described herein, it is contemplated that alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc. without departing from the spirit and/or scope of the innovation as described in detail. These alternative embodiments are to be included within the spirit and scope of the innovation as described and claimed herein.\|[0071] Although the subject matter has been described in language specific to structural features or methodological acts, it is to be understood that the subject matter of the appended claims is not necessarily limited to the specific features or acts described above. Rather, the specific features and acts described above are disclosed as example aspects.\|[0072] Various operations of aspects are provided herein. The order in which one or more or all of the operations are described should not be construed as to imply that these operations are necessarily order dependent. Alternative ordering will be appreciated based on this description. Further, not all operations may necessarily be present in each aspect provided herein.\|[0073] As used in this application, “or” is intended to mean an inclusive “or” rather than an exclusive “or”. Further, an inclusive “or” may include any combination thereof (e.g., A, B, or any combination thereof). In addition, “a” and “an” as used in this application are generally construed to mean “one or more” unless specified otherwise or clear from context to be directed to a singular form. Additionally, at least one of A and B and/or the like generally means A or B or both A and B. Further, to the extent that “includes”, “having”, “has”, “with”, or variants thereof are used in either the detailed description or the claims, such terms are intended to be inclusive in a manner similar to the term “comprising”.\|[0074] Further, unless specified otherwise, “first”, “second”, or the like are not intended to imply a temporal aspect, a spatial aspect, an ordering, etc. Rather, such terms are merely used as identifiers, names, etc. for features, elements, items, etc. For example, a first channel and a second channel generally correspond to channel A and channel B or two different or two identical channels or the same channel. Additionally, “comprising”, “comprises”, “including”, “includes”, or the like generally means comprising or including, but not limited thereto.\|[0075] Further, the term “in” as used to describe an object with respect to a given direction (e.g., an edge extended in a left-right direction) is intended to denote an orientation that is substantially parallel to the specified direction. In contrast, the term “along” as used to describe an object with respect to a given direction (e.g., an edge extended along a vertical direction) is intended to indicate that a feature or element possesses a common vector component in that direction, even if its overall alignment is not strictly parallel.\|[0076] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.	Family Number\|(116035972)\|116035972\|Object of Invention\|(US20250297409 A1)\|According to another aspect, infill for a synthetic turf system includes carbon sequestration sand.\|In accordance with varying embodiments discussed herein, there is provided an artificial turf system that utilizes a material derived from one or more types of carbon sequestration sands, including, for example and without limitation, wollastonite sand (general formula CaSiO_3), limestone, basalt, or the like.\|(WO2025199637 A1)\|According to another aspect, a method of preparing a synthetic turf system includes dispersing carbon sequestration sand over a top portion of turf fibers, where the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a bicarbonate or carbonate with rainwater traveling through infill.\|According to another aspect, infill for a synthetic turf system includes carbon sequestration sand.\|In yet another aspect, a layer of carbon sequestration sand may be positioned on a geotextile or subgrade layer.\|Abstract\|(US20250297409 A1)\|A synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|(WO2025199637 A1)\|A synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|Title\|(US20250297409 A1)\|Carbon sequestration sand-based material for synthetic turf\|Carbon sequestration sand-based material for synthetic turf fields\|(WO2025199637 A1)\|Carbon sequestration sand-based material for synthetic turf\|Advantages / Prev. Drawbacks\|(US20250297409 A1)\|Furthermore, it will be appreciated that by placing the carbon sequestration sand 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air.\|It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|(WO2025199637 A1)\|It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1 -8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|Independent Claims\|(US20250297409 A1)\| (...) wherein the one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\| (...) carbon sequestration sand including silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh; and organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\| (...) dispersing carbon sequestration sand over a top portion of turf fibers, wherein the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|(WO2025199637 A1)\|1. A synthetic turf system comprising: a backing; turf fibers extended upward from the backing; one or more infill layers positioned above the backing, below a top portion of the turf fibers; wherein the one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|12. Infill for a synthetic turf system, the infill comprising: carbon sequestration sand including silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about (...) particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|17. A method of preparing a synthetic turf system, the method comprising: dispersing carbon sequestration sand over a top portion of turf fibers, wherein the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|	Chemical engineering\|Civil engineering\|Environmental technology\|Textile and paper machines	D02G-003/44/5\|D10B-2403/02421\|D10B-2505/202\|E01C-013/02\|E01C-013/08		D02G-003/44/5\|D10B-2403/02421\|D10B-2505/202\|E01C-013/02\|E01C-013/08	B01D-053/02\|B01D-053/62\|B01J-020/10\|D02G-003/44\|E01C-013/08	B01D-053/02\|B01D-053/62\|B01J-020/10\|D02G-003/44\|E01C-013/08					WO2020142232\|WO2021204310\|US20220049450	WO2020142232 89636781 WHO=Examiner SELF=N CAT=X CAT=Y CAT=A\|WO2021204310 96459586 WHO=Examiner SELF=N CAT=X CAT=Y\|US20220049450 98730333 WHO=Examiner SELF=N CAT=X CAT=A		WO2021204310; WO2020142232; US20220049450\|		PENDING	(US20250297409)\|PENDING\|(WO2025/199637)\|PENDING	ALIVE	(US20250297409)\|ALIVE\|(WO2025/199637)\|ALIVE	(US20250297409)\|LEGAL DETAILS FOR US20250297409\|Actual or expected expiration date=2045-03-25\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-03-25\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19089278\|Application date=2025-03-25\|Standardized application number=2025US-19089278\|Event publication date=2025-03-25\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-03-25\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-03-25\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 58213-00345\|Event publication date=2025-03-25\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 136458\|Event publication date=2025-03-25\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2025-03-25\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-03-25\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2025-03-25\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-03-25\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-03-31\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:SMOLETT, JASON;HABIB, ERIC;CHISAM, CHRISTOPHER;SIGNING DATES FROM 20250320 TO 20250326\|Reel/frame:070683/0386\|OWNER:TARKETT SPORTS CANADA INC., CANADA\|Event publication date=2025-04-01\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-04-28\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-04-28\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-07-15\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2025-09-25\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250297409\|Publication stage code=A1\|Publication date=2025-09-25\|Standardized publication number=US20250297409\|Event publication date=2025-09-25\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|(WO2025/199637)\|LEGAL DETAILS FOR WO2025/199637\|Actual or expected expiration date=2027-09-25\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-03-25\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOCA2025/050423\|Application date=2025-03-25\|Standardized application number=2025WO-CA50423\|Event publication date=2025-10-02\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/199637\|Publication stage code=A1\|Publication date=2025-10-02\|Standardized publication number=WO2025199637\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2045-03-25\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP25778857\|Event publication date=2025-11-12\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP	(WO2025/199637)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/199637)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/199637)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/199637)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/199637)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UY, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(US20250297409)\|US\|(WO2025/199637)\|WO; EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcP1jvMh5Li0oTkuDREcUBY0JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023019215&ekey=1918&xpn=US20250297409&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19089278/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=zeXk%252BPpISmSlgNU07Y9GJ8RHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2025/199637)\|CA\|(US20250297409)\|CA	(WO2025/199637)\|NAME=TARKETT SPORTS CANADA INC. 7445 Cote-de-Liesse Rd. Suite 200 Montreal, Québec H4T 1G2 , COUNTRY=CA\|(US20250297409)\|NAME=Tarkett Sports Canada Inc. , CITY=Montreal , COUNTRY=CA	(WO2025/199637)\|CA	(WO2025/199637)\|NAME=YIP, Vincent Suite 2400 745 Thurlow Street Vancouver, British Columbia V6E 0C5 , POSTCODE=V6E 0C5 , COUNTRY=CA	(US20250297409)\|CA; CA; US\|(WO2025/199637)\|CA; CA; US	(US20250297409)\|NAME=Smolett Jason, CITY=Kirkland, COUNTRY=CA \|NAME=Habib Eric, CITY=Pierrefonds, COUNTRY=CA \|NAME=Chisam Christopher, CITY=Granite Bay, STATE=CA , COUNTRY=US\|(WO2025/199637)\|NAME=SMOLETT, Jason 71 Rondeau Kirkland, Québec H9H 4J2, POSTCODE=H9H 4J2, COUNTRY=CA \|NAME=HABIB, Eric 4967 Saint Barnabas Pierrefonds, Québec H8Z 3B9, POSTCODE=H8Z 3B9, COUNTRY=CA \|NAME=CHISAM, Christopher 9792 Swan Lake Drive Granite Bay, California 95746, POSTCODE=95746, COUNTRY=US	(WO2025/199637)\|9\|(US20250297409)\|9	2	2					(US20250297409)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,12,17\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|\|(WO2025/199637)\|Number of Claims: NCL=20\|Extended kind: EXTK=x\|	(US20250297409)\|Provisional Appl: US63/569,558 FDD=2024-03-25 [2024US-63569558]	(US20250297409)\|ENGLISH (ENG)	(WO2025199637)\|Patent\|(US20250297409)\|Patent	Titre: (US20250297409)\|Carbon sequestration sand-based material for synthetic turf fields Résumé: (US20250297409)\|A synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.	8	Abstract	gpt-4o-mini	no	The article focuses on a synthetic turf system that includes carbon sequestration sand, which does not relate to the accelerated weathering of minerals for CO₂ capture.
14	CN202411779739	CN202411779739	CN119666501	113895166	CN119666501 A 2025-03-21 [CN119666501]	2024-12-05	2024-12-05	2025-03-21		(CN119666501)\|2044-12-05	(CN119666501)\|Method for determining total organic carbon content in rock	(CN119666501)\|The invention discloses a method for determining the total organic carbon content in rock, which comprises the following steps: grinding a rock sample, and weighing a preset mass of crushed rock sample; putting the weighed crushed rock sample into a container, and adding an excessive hydrochloric acid solution into the container; washing the crushed rock sample treated by hydrochloric acid with distilled water until the crushed rock sample is neutral; picking the cleaned broken rock sample under a microscope; burning the broken rock sample with the elemental carbon removed in high-temperature oxygen flow, and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample. The method has the beneficial effects that after inorganic carbon in the sample is removed through diluted hydrochloric acid, the sample is picked under a microscope, simple substance carbon in the crushed rock sample is removed, then the crushed rock sample with the simple substance carbon removed is combusted in high-temperature oxygen flow, the total organic carbon is converted into carbon dioxide, the content of the total organic carbon is obtained through an infrared detector, and the content of the total organic carbon in the crushed rock sample is calculated. And the accuracy of the total organic carbon content determination result can be improved.	SHAANXI YANCHANG PETROLEUM	(CN119666501)\|SHAANXI YANCHANG PETROLEUM (GROUP) CO. LTD. ([CN])	LIU SHUANGSHUANG\|CUI PENGXING\|LIU LILI\|KANG SHENGSONG\|ZHAO XUESI\|WANG TAO\|ZHU TONGTONG	(CN119666501)\|LIU SHUANGSHUANG\|CUI PENGXING\|LIU LILI\|KANG SHENGSONG\|ZHAO XUESI\|WANG TAO\|ZHU TONGTONG	(CN119666501)\|HE SHAN;XIAN YINUO PATENT AGENT CO. LTD.\|Reg. Nb: 61220	(CN119666501)\|However, the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, for example, for the coal-bearing formation, the rock sample may contain elemental carbon such as graphite and amorphous carbon, and the elemental carbon is stable at normal temperature and does not react with the dilute hydrochloric acid, so that the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, which results in a higher content of the measured total organic carbon.\|	(CN119666501)\|1. A method for determining total organic carbon content in rock, comprising: s1, grinding a rock sample, and weighing rock fragments with preset mass; S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; S4, picking the cleaned crushed rock sample under a microscope, and removing simple substance carbon in the crushed rock sample; And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|	(CN119666501)\|The invention discloses a method for measuring total organic carbon content in rock, which comprises the steps of grinding a rock sample, weighing rock fragments with preset mass, placing the weighed rock fragments into a container, adding excessive hydrochloric acid solution into the container, washing the rock fragments subjected to hydrochloric acid treatment to be neutral through distilled water, picking the washed rock fragments under a microscope, burning the rock fragments subjected to simple substance carbon removal in high-temperature oxygen flow, and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample.\|The invention relates to the technical field of total organic carbon content measurement, in particular to a method for measuring total organic carbon content in rock.\|the invention provides a method for measuring the content of total organic carbon in rock, which comprises the following steps:\|	(CN119666501)\|TOTAL ORGANIC CARBON(100,55)\|TOTAL ORGANIC CARBON CONTENT(100,29)\|ROCK(100,28)\|WASHED ROCK FRAGMENT(100,1)\|ROCK SAMPLE(95,15)\|CRUSHED ROCK SAMPLE(84,23)\|WEIGHED ROCK(84,1)\|ELEMENTAL CARBON(72,15)\|MICROSCOPIC PICKING(62,7)\|TRANSPARENT PIPE(61,10)\|MICROSCOPE(58,22)\|WEIGHED CRUSHED ROCK(56,3)\|PRESET DEVICE MASS(53,4)\|CONTENT MEASUREMENT(51,4)\|CLEANED CRUSHED ROCK SAMPLE(50,3)\|BUFFER TANK(49,18)\|BURNER(49,18)\|GRAVEL(47,13)\|HYDROCHLORIC ACID(46,20)\|SUCKING SUBSTANCE CARBON(46,1)\|SUCKING ELEMENTAL CARBON PARTICLE(43,3)\|SUBSTANCE CARBON(42,13)\|SCREW HOLE(42,9)\|SUBSTANCE CARBON REMOVAL(42,4)\|ENTIRE INORGANIC CARBON(42,2)\|SLIDING SLEEVE(39,22)\|INFRARED DETECTOR(38,20)\|WEIGHED CRUSHED ROCK SAMPLE(38,2)\|INORGANIC CARBON(37,7)\|HYDROCHLORIC ACID TREATMENT(36,8)\|OUTPUT PIPE(35,10)\|CACHE TANK(33,2)\|OXYGEN STREAM(32,3)\|BLOCKING NET(32,2)\|HYDROCHLORIC ACID SOLUTION(31,4)\|GAS OUTLET(30,9)\|COAL BEARING FORMATION(30,1)\|HOLE INCLINATION(29,6)\|CONTENT DETECTION(28,7)\|IGNITER(28,7)\|COMBUSTION TABLE(27,6)\|GRAVEL PLACEMENT(27,3)\|OXYGEN FLOW(27,3)\|OXYGEN INLET(25,5)\|CLOSED COMBUSTION CAVITY(25,2)\|GENERATED CARBON DIOXIDE CONTENT(25,1)\|GENERATED CARBON DIOXIDE(24,5)\|CARBON DIOXIDE(22,17)\|GAS INLET(22,6)\|GAS EXHAUST PIPE(21,6)\|AIR INLET(19,6)\|DISTILLED WATER(19,5)\|GRAPHITE(19,4)\|CROSS ROD(18,8)\|THREADED CONNECTION(18,6)\|SUCTION PUMP(17,8)\|OXYGEN TANK(16,8)\|PLATE POSITION(16,2)\|OUTLET VALVE(15,13)\|AMORPHOUS CARBON(15,4)\|GAS GUIDE VALVE(15,3)\|PLACING PLATE(14,3)\|OUTPUT VALVE(13,5)\|GAS EXHAUST VALVE(13,3)\|OBJECTIVE LENS(13,3)\|WATER OUTLET(13,3)\|TUNGSTEN PARTICLE COSOLVENT(12,1)\|WEIGHED ROCK FRAGMENT MASS(12,1)\|AIR PUMP(11,10)\|EVALUATING ABUNDANCE(10,1)\|SCIENTIFIC APPARATUS PLATE(9,4)\|AUXILIARY PIPELINE(9,1)\|MONTANT BUTT(9,1)\|SCRAP IRON COSOLVENT(9,1)\|ADJUSTED POSITION(8,3)\|HORIZONTAL DIRECTION(8,3)\|PRESSURE DETECTING MEMBER(8,3)\|WATER BATH TEMPERATURE(7,3)\|OBJECT POSITION(7,2)\|ABSORBING SUBSTANCE CARBON(7,1)\|HORIZONTAL POLE BUTT(7,1)\|ROCK POWDER(7,1)\|SEALED COMBUSTION CAVITY(7,1)\|AIR OUTLET(6,3)\|	(CN119666501)\|1. A method for determining total organic carbon content in rock, comprising:\| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope, and removing simple substance carbon in the crushed rock sample; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|2. The method for measuring the content of total organic carbon in rock according to claim 1, wherein in the step S1, the mass of the weighed crushed rock sample is 0.01-1.00g.\|3. The method for measuring the total organic carbon content in rock according to claim 1, wherein in the step S2, the container is placed in a water bath, and the temperature of the water bath is controlled to be 60-80 ℃.\|4. The method according to claim 1, wherein in the step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by a sample washing device, the sample washing device comprises a cylinder and a screen, the upper end of the cylinder is provided with an opening, the lower end of the cylinder is provided with a water outlet, and the screen is detachably mounted at the opening of the upper end of the cylinder.\|5. The method according to claim 1, wherein in the step S4, the cleaned crushed rock is picked by a microscopic picking device, so as to remove the elemental carbon in the crushed rock, the microscopic picking device comprises a base, a placing plate, a microscope, a position adjusting mechanism and a picking mechanism, the microscope is located above the base, the placing plate is used for placing the crushed rock on the base, the position adjusting mechanism is connected with the microscope and used for adjusting the position of an objective lens of the microscope, and the picking mechanism is used for sucking the elemental carbon particles.\|6. The method for measuring the total organic carbon content in rock according to claim 5, wherein the position adjusting mechanism comprises a vertical rod, a vertical sliding sleeve, a vertical screw, a transverse sliding sleeve, a cross rod, a transverse screw and a bracket, wherein the lower end of the vertical rod is fixed on the base, the vertical sliding sleeve is slidably sleeved on the vertical rod and extends along the vertical direction, a first screw hole is formed in the vertical sliding sleeve, the vertical screw is in threaded connection with the first screw hole and is used for being abutted to the vertical rod, the transverse sliding sleeve is fixed on the vertical sliding sleeve and extends along the horizontal direction, the cross rod is slidably inserted in the transverse sliding sleeve, a second screw hole is formed in the transverse sliding sleeve, the transverse screw is in threaded connection with the second screw hole and is used for being abutted to the cross rod, the bracket is fixed on one end of the cross rod, and the bracket is fixedly connected with a microscope.\|7. The method for measuring the total organic carbon content in rock according to claim 6, wherein the bracket is provided with an inclined hole which is obliquely arranged, the sampling mechanism comprises a transparent pipe, a blocking net, a suction pump and a connecting hose, the transparent pipe is slidably inserted into the inclined hole, the lower end of the transparent pipe is used for sucking the simple substance carbon on the object placing plate, the blocking net is fixed at the lower end of the transparent pipe, and the inlet of the suction pump is communicated with the upper end of the transparent pipe through the connecting hose.\|8. The method for determining the total organic carbon content in rock according to claim 1, wherein in the step S4, the crushed rock sample from which the elemental carbon is removed is burned in a high-temperature oxygen stream by a total organic carbon content detection device, and the content of carbon dioxide generated is detected by an infrared detector, so as to obtain the total organic carbon content of the rock sample, and the total organic carbon content detection device comprises a burner, an oxygen introducing mechanism, a buffer mechanism and the infrared detector;\| The burner comprises a burner body, a combustion table and an igniter, wherein a closed combustion cavity is formed in the burner body, an air inlet communicated with the combustion cavity is formed in one end of the burner body, an air outlet communicated with the combustion cavity is formed in the other end of the burner body, the combustion table is arranged in the burner body, and the igniter is arranged in the burner body; \| the oxygen inlet mechanism comprises an oxygen tank, an outlet valve, an air pump and an output pipe, the outlet valve is arranged at the outlet of the oxygen tank, the inlet of the air pump is communicated with the outlet valve, the outlet of the air pump is communicated with one end of the output pipe, the other end of the output pipe is communicated with the air inlet, and the output pipe is provided with the output valve; \| The buffer mechanism comprises a buffer tank and a vacuum pump, wherein a gas inlet is formed in one end of the buffer tank, a gas outlet is formed in the other end of the buffer tank, the gas inlet is communicated with the gas outlet through a conduit, a gas guide valve is arranged on the conduit, the inlet of the vacuum pump is communicated with the gas outlet through a gas exhaust pipe, and the gas exhaust pipe is provided with a gas exhaust valve; \| The infrared detector is arranged in the cache tank. \|9. The method for measuring the total organic carbon content in rock according to claim 8, wherein a one-way valve is further arranged on the output pipe.\|10. The method for measuring the total organic carbon content in rock according to claim 8, wherein a pressure detecting member is provided on the buffer tank.	(CN119666501)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of total organic carbon content measurement, in particular to a method for measuring total organic carbon content in rock.\|BACKGROUND ART\|[0002] The total organic carbon content (TOC) in rock refers to the mass of organic carbon per mass of rock, typically expressed as mass fraction (%). The index has important significance in geology and oil and gas exploration, and is commonly used for evaluating the abundance, maturity and hydrocarbon production potential of organic matters of hydrocarbon source rocks.\|[0003] The existing method for measuring the content of the total organic carbon in the rock is to remove inorganic carbon in a sample by using dilute hydrochloric acid, burn the inorganic carbon in high-temperature oxygen flow, convert the total organic carbon into carbon dioxide, and send the content of the total organic carbon through an infrared detector.\|[0004] However, the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, for example, for the coal-bearing formation, the rock sample may contain elemental carbon such as graphite and amorphous carbon, and the elemental carbon is stable at normal temperature and does not react with the dilute hydrochloric acid, so that the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, which results in a higher content of the measured total organic carbon.\|DISCLOSURE\|Disclosure of Invention\|[0005] The invention aims to overcome the technical defects, and provides a method for measuring the total organic carbon content in rock, which solves the technical problem that the content of the measured total organic carbon is higher because simple substance carbon such as graphite, amorphous carbon and the like possibly contained in a rock sample is not removed in the method for measuring the total organic carbon content in the prior art.\|[0006] In order to achieve the technical purpose, the invention adopts the following technical scheme:\| the invention provides a method for measuring the content of total organic carbon in rock, which comprises the following steps: \| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope, and removing simple substance carbon in the crushed rock sample; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|[0007] In some embodiments, in step S1, the mass of the weighed rock fragments is 0.01-1.00g.\|[0008] In some embodiments, in step S2, the container is placed in a water bath, and the temperature of the water bath is controlled to be 60-80 ℃.\|[0009] In some embodiments, in step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by a sample washing device, where the sample washing device includes a cylinder and a screen, an opening at an upper end of the cylinder is provided, a water outlet is provided at a lower end of the cylinder, and the screen is detachably mounted at the opening at the upper end of the cylinder.\|[0010] In some embodiments, in step S4, the cleaned crushed rock is picked by a microscopic picking device, so as to remove elemental carbon in the crushed rock, where the microscopic picking device includes a base, a placing plate, a microscope, a position adjusting mechanism and a picking mechanism, the microscope is located above the base, the placing plate is used for placing the crushed rock on the base, the position adjusting mechanism is connected with the microscope and used for adjusting the position of an objective lens of the microscope, and the picking mechanism is used for sucking elemental carbon particles.\|[0011] In some embodiments, the position adjustment mechanism includes montant, vertical sliding sleeve, vertical screw, horizontal sliding sleeve, horizontal pole, horizontal screw and support, the lower extreme of montant is fixed in the base, vertical sliding sleeve locates the montant to extend along vertical direction, set up first screw on the vertical sliding sleeve, vertical screw threaded connection in first screw, and be used for with montant butt, horizontal sliding sleeve is fixed in vertical sliding sleeve to extend along the horizontal direction, the horizontal pole slides and inserts and locate in the horizontal sliding sleeve, the second screw has been seted up on the horizontal sliding sleeve, horizontal screw threaded connection in the second screw, and be used for with the horizontal pole butt, the support is fixed in the one end of horizontal pole, the support with microscope fixed connection.\|[0012] In some embodiments, the support is provided with an inclined hole arranged obliquely, the sampling mechanism comprises a transparent pipe, a blocking net, a suction pump and a connecting hose, the transparent pipe is slidably inserted into the inclined hole, the lower end of the transparent pipe is used for absorbing simple substance carbon on the object placing plate, the blocking net is fixed at the lower end of the transparent pipe, and an inlet of the suction pump is communicated with the upper end of the transparent pipe through the connecting hose.\|[0013] In some embodiments, in the step S4, the crushed rock sample after removing the elemental carbon is burned in a high-temperature oxygen stream by a total organic carbon content detection device, and the content of the generated carbon dioxide is detected by an infrared detector, so as to obtain the total organic carbon content of the rock sample, where the total organic carbon content detection device includes a burner, an oxygen inlet mechanism, a buffer mechanism and the infrared detector;\| The burner comprises a burner body, a combustion table and an igniter, wherein a closed combustion cavity is formed in the burner body, an air inlet communicated with the combustion cavity is formed in one end of the burner body, an air outlet communicated with the combustion cavity is formed in the other end of the burner body, the combustion table is arranged in the burner body, and the igniter is arranged in the burner body; \| the oxygen inlet mechanism comprises an oxygen tank, an outlet valve, an air pump and an output pipe, the outlet valve is arranged at the outlet of the oxygen tank, the inlet of the air pump is communicated with the outlet valve, the outlet of the air pump is communicated with one end of the output pipe, the other end of the output pipe is communicated with the air inlet, and the output pipe is provided with the output valve; \| The buffer mechanism comprises a buffer tank and a vacuum pump, wherein a gas inlet is formed in one end of the buffer tank, a gas outlet is formed in the other end of the buffer tank, the gas inlet is communicated with the gas outlet through a conduit, a gas guide valve is arranged on the conduit, the inlet of the vacuum pump is communicated with the gas outlet through a gas exhaust pipe, and the gas exhaust pipe is provided with a gas exhaust valve; \| The infrared detector is arranged in the cache tank. \|[0014] In some embodiments, a one-way valve is also provided on the output tube.\|[0015] In some embodiments, the buffer tank is provided with a pressure detecting member thereon.\|[0016] Compared with the prior art, the method for measuring the total organic carbon content in the rock has the beneficial effects that: removing inorganic carbon in a sample through dilute hydrochloric acid, picking under a microscope to remove simple substance carbon in the crushed rock sample, burning the crushed rock sample after removing the simple substance carbon in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and obtaining the content of the total organic carbon through an infrared detector.\|DRAWINGS DESCRIPTION\|[0017] Fig. 1 is a schematic structural diagram of a method for measuring total organic carbon content in rock according to an embodiment of the present invention.\|[0018] Fig. 2 is a schematic structural view of the sample washing apparatus used in step S3 in fig. 1.\|[0019] Fig. 3 is a schematic structural diagram of a microscopic picking device used in step S4 in fig. 1.\|[0020] Fig. 4 is a partial enlarged view of the area a in fig. 3.\|[0021] FIG. 5 is a schematic view of the microscope sampling device of FIG. 3 when the transparent tube is lifted.\|[0022] Fig. 6 is a schematic view of the microscope sampling device of fig. 5 at another perspective.\|[0023] Fig. 7 is a schematic structural diagram of the total organic carbon content detecting device used in step S5 in fig. 1.\|[0024] The reference numerals are 100-sample cleaning device, 110-cylinder, 111-water outlet, 120-screen, 200-microscopic sample picking device, 210-base, 220-object placing plate, 230-microscope, 240-position adjusting mechanism, 241-vertical rod, 242-vertical sliding sleeve, 243-vertical screw, 244-horizontal sliding sleeve, 245-horizontal rod, 246-horizontal screw, 247-bracket, 250-sample picking mechanism, 251-transparent tube, 252-blocking net, 300-total organic carbon content detecting device, 310-burner, 311-furnace body, 312-combustion table, 313-igniter, 320-oxygen inlet mechanism, 321-oxygen tank, 322-outlet valve, 323-air pump, 324-output pipe, 325-output valve, 326-one-way valve, 330-buffering mechanism, 331-buffering tank, 3311-pressure detecting piece, 332-vacuum pump, 333-conduit, 334-air guide valve, 335-air suction tube, 336-suction valve, 340-infrared detector.\|INVENTION MODE\|Detailed Description\|[0025] The present invention will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0026] In order to solve the technical problem that the content of the measured total organic carbon is higher because simple substance carbon such as graphite and amorphous carbon possibly contained in a rock sample is not removed in the total organic carbon content measuring method, the invention provides the total organic carbon content measuring method in the rock, and the accuracy of measuring the total organic carbon content can be improved.\|[0027] Referring to fig. 1, fig. 1 is a flow chart of a method for determining total organic carbon content in rock according to an embodiment of the invention, the method for determining total organic carbon content in rock includes the following steps:\| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope to remove the simple substance carbon in the crushed rock sample, wherein the simple substance carbon in the rock is mainly graphite and amorphous carbon which are black, and the rock powder is usually light, so that the simple substance carbon can be easily identified and removed under the microscope; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|[0028] According to the technical scheme provided by the invention, after inorganic carbon in a sample is removed through dilute hydrochloric acid, sample picking is performed under a microscope to remove simple substance carbon in the rock fragments, then the rock fragments after simple substance carbon removal are combusted in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and the content of the total organic carbon is obtained through an infrared detector.\|[0029] In one embodiment, referring to fig. 1, in the step S1, the rock sample is ground to a particle size of less than 0.2mm, the mass of the ground sample is not less than 10g, and in the step S1, the mass of the weighed crushed rock sample is 0.01-1.00g, and is accurate to 0.0001g.\|[0030] In one embodiment, referring to fig.1, in the step S2, the container is placed in a water bath, the temperature of the water bath is controlled to be 60-80 ℃, and the sample is dissolved for more than 2 hours until the reaction is complete.\|[0031] In one embodiment, referring to fig. 1 and 2, in step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by the sample washing device 100, the sample washing device 100 includes a cylinder 110 and a screen 120, an upper end opening of the cylinder 110 is disposed, a water outlet 111 is disposed at a lower end of the cylinder 110, and the screen 120 is detachably mounted at the upper end opening of the cylinder 110. In use, the crushed rock sample after hydrochloric acid treatment is poured into the screen 120, and distilled water boiled is continuously introduced into the screen until the pH value of the crushed rock sample is neutral.\|[0032] In one embodiment, referring to fig. 1 and 3, in step S4, the cleaned crushed rock is picked by a microscopic picking device 200 to remove elemental carbon in the crushed rock, the microscopic picking device 200 includes a base 210, a placing plate 220, a microscope 230, a position adjusting mechanism 240, and a picking mechanism 250, the microscope 230 is located above the base 210, the placing plate 220 is used for placing the crushed rock on the base 210, the position adjusting mechanism 240 is connected with the microscope 230 and is used for adjusting the position of an objective lens of the microscope 230, and the picking mechanism 250 is used for sucking elemental carbon particles.\|[0033] In one embodiment, please refer to fig. 3-6, the position adjusting mechanism 240 includes a vertical rod 241, a vertical sliding sleeve 242, a vertical screw 243, a horizontal sliding sleeve 244, a cross rod 245, a horizontal screw 246 and a support 247, wherein the lower end of the vertical rod 241 is fixed in the base 210, the vertical sliding sleeve 242 is slidably sleeved on the vertical rod 241 and extends along the vertical direction, a first screw hole is formed in the vertical sliding sleeve 242, the vertical screw 243 is in threaded connection with the first screw hole and is used for being in butt joint with the vertical rod 241, the horizontal sliding sleeve 244 is fixed in the vertical sliding sleeve 242 and extends along the horizontal direction, the cross rod 245 is slidably inserted in the horizontal sliding sleeve 244, a second screw hole is formed in the horizontal sliding sleeve 244, the horizontal screw 246 is in threaded connection with the second screw hole and is used for being in butt joint with the cross rod 245, the support 247 is fixed at one end of the cross rod 245, the support 247 is fixedly connected with the microscope 230, and when in use, the vertical screw 243 is unscrewed, namely, the vertical sliding sleeve 242 is in threaded connection with the first screw hole, and is used for being in threaded connection with the vertical sliding sleeve 241, so as to enable the vertical sliding sleeve 241 to rotate around the microscope 241, thereby enable the vertical sliding sleeve 241 to rotate around the vertical rod 241, and the microscope 241 to reach the position of the microscope 230, and the position of the microscope 230 can be changed, and the position of the microscopic plate 220 can be different from the position of the microscopic plate 220, and the microscopic plate 220 can be in turn, or the position of the microscopic plate 220, and the position can be changed.\|[0034] In one embodiment, referring to fig. 3-6, the support 247 is provided with an inclined hole, the sample picking mechanism 250 includes a transparent tube 251, a blocking net 252, a suction pump (not shown) and a connection hose (not shown), the transparent tube 251 is slidably inserted into the inclined hole, the lower end of the transparent tube 251 is used for sucking the elemental carbon on the object placing plate 220, the blocking net 252 is fixed at the lower end of the transparent tube 251, the inlet of the suction pump is communicated with the upper end of the transparent tube 251 through the connection hose, when in use, the lower end of the transparent tube 251 is aligned with the elemental carbon, then the suction pump is started, the elemental carbon is sucked into the transparent tube 251 by the blocking net 252, then the transparent tube 251 is lifted, then the material receiving box is placed at the lower end of the transparent tube 251, then the suction pump is closed, and the elemental carbon in the transparent tube 251 falls into the material receiving box under the action of gravity, thereby removing the elemental carbon.\|[0035] In one embodiment, referring to fig. 1 and 7, in step S4, a crushed rock sample from which elemental carbon is removed is burned in a high-temperature oxygen stream by a total organic carbon content detection device 300, and the content of carbon dioxide generated is detected by an infrared detector to obtain the total organic carbon content of the rock sample, where the total organic carbon content detection device 300 includes a burner 310, an oxygen inlet mechanism 320, a buffer mechanism 330, and an infrared detector 340;\| the burner 310 comprises a burner body 311, a burner table 312 and an igniter 313, wherein a sealed combustion cavity is arranged in the burner body 311, an air inlet communicated with the combustion cavity is formed in one end of the burner body 311, an air outlet communicated with the combustion cavity is formed in the other end of the burner body 311, the burner table 312 is arranged in the burner body 311, and the igniter 313 is arranged in the burner body 311; \| The oxygen inlet mechanism 320 comprises an oxygen tank 321, an outlet valve 322, an air pump 323 and an output pipe 324, the outlet valve 322 is arranged at the outlet of the oxygen tank 321, the inlet of the air pump 323 is communicated with the outlet valve 322, the outlet of the air pump 323 is communicated with one end of the output pipe 324, the other end of the output pipe 324 is communicated with the air inlet, and the output pipe 324 is provided with an output valve 325; \| The buffer mechanism 330 comprises a buffer tank 331 and a vacuum pump 332, wherein a gas inlet is formed at one end of the buffer tank 331, a gas outlet is formed at the other end of the buffer tank 331, the gas inlet is communicated with the gas outlet through a conduit 333, a gas guide valve 334 is arranged on the conduit 333, an inlet of the vacuum pump 332 is communicated with the gas outlet through a gas exhaust pipe 335, and a gas exhaust valve 336 is arranged on the gas exhaust pipe 335; \| the infrared detector 340 is disposed in the buffer tank 331. \|[0036] The detection flow of the total organic carbon content detection device 300 is as follows:\| (1) Uniformly mixing the crushed rock sample after removing the simple substance carbon with the scrap iron cosolvent and the tungsten particle cosolvent, and placing the mixture in a combustion table 312; \| (2) Vacuumizing, closing the outlet valve 322, opening the output valve 325, the air guide valve 334 and the air extraction valve 336, and then opening the vacuum pump 332, wherein the vacuum pump vacuumizes the buffer tank 331, the oxygen tank 321 and the pipeline; \| (3) Oxygen is introduced, the air extraction valve 336 and the air guide valve 334 are closed, the outlet valve 322 is opened, and sufficient oxygen is introduced into the combustion chamber; \| (4) The igniter 313 ignites the sample on the combustion table 312, continuously introduces oxygen, and then opens the outlet valve 322 to introduce the generated gas into the buffer tank 331; \| (5) After full combustion, the output valve 325 is closed, combustion is stopped, after the system is stable, the carbon dioxide concentration in the buffer tank 331 is detected through the infrared detector 340, the carbon dioxide concentration in the buffer tank 331 is equal to the carbon dioxide concentration in the furnace body 311, the total amount of carbon dioxide generated by combustion can be obtained according to the carbon dioxide concentration multiplied by the total volume of the buffer tank 331, the furnace body 311 and the auxiliary pipeline, the total amount of organic carbon in the crushed rock sample is further obtained, and the total organic carbon content in the crushed rock sample can be obtained by dividing the total amount by the mass of the crushed rock sample. \|[0037] In one embodiment, referring to fig. 1 and 7, the output pipe 324 is further provided with a check valve 326, so as to avoid reverse flow of the gas.\|[0038] In one embodiment, referring to fig. 1 and 7, a pressure detecting member 3311 is provided on the buffer tank 331 to facilitate control of the reaction pressure.\|[0039] According to the technical scheme provided by the invention, after inorganic carbon in a sample is removed through dilute hydrochloric acid, sample picking is performed under a microscope to remove simple substance carbon in the rock fragments, then the rock fragments after simple substance carbon removal are combusted in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and the content of the total organic carbon is obtained through an infrared detector.\|[0040] The above-described embodiments of the present invention do not limit the scope of the present invention. Any other corresponding changes and modifications made in accordance with the technical idea of the present invention shall be included in the scope of the claims of the present invention.	(CN119666501)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of total organic carbon content measurement, in particular to a method for measuring total organic carbon content in rock.\|BACKGROUND ART\|[0002] The total organic carbon content (TOC) in rock refers to the mass of organic carbon per mass of rock, typically expressed as mass fraction (%). The index has important significance in geology and oil and gas exploration, and is commonly used for evaluating the abundance, maturity and hydrocarbon production potential of organic matters of hydrocarbon source rocks.\|[0003] The existing method for measuring the content of the total organic carbon in the rock is to remove inorganic carbon in a sample by using dilute hydrochloric acid, burn the inorganic carbon in high-temperature oxygen flow, convert the total organic carbon into carbon dioxide, and send the content of the total organic carbon through an infrared detector.\|[0004] However, the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, for example, for the coal-bearing formation, the rock sample may contain elemental carbon such as graphite and amorphous carbon, and the elemental carbon is stable at normal temperature and does not react with the dilute hydrochloric acid, so that the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, which results in a higher content of the measured total organic carbon.\|DISCLOSURE\|Disclosure of Invention\|[0005] The invention aims to overcome the technical defects, and provides a method for measuring the total organic carbon content in rock, which solves the technical problem that the content of the measured total organic carbon is higher because simple substance carbon such as graphite, amorphous carbon and the like possibly contained in a rock sample is not removed in the method for measuring the total organic carbon content in the prior art.\|[0006] In order to achieve the technical purpose, the invention adopts the following technical scheme:\| the invention provides a method for measuring the content of total organic carbon in rock, which comprises the following steps: \| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope, and removing simple substance carbon in the crushed rock sample; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|[0007] In some embodiments, in step S1, the mass of the weighed rock fragments is 0.01-1.00g.\|[0008] In some embodiments, in step S2, the container is placed in a water bath, and the temperature of the water bath is controlled to be 60-80 ℃.\|[0009] In some embodiments, in step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by a sample washing device, where the sample washing device includes a cylinder and a screen, an opening at an upper end of the cylinder is provided, a water outlet is provided at a lower end of the cylinder, and the screen is detachably mounted at the opening at the upper end of the cylinder.\|[0010] In some embodiments, in step S4, the cleaned crushed rock is picked by a microscopic picking device, so as to remove elemental carbon in the crushed rock, where the microscopic picking device includes a base, a placing plate, a microscope, a position adjusting mechanism and a picking mechanism, the microscope is located above the base, the placing plate is used for placing the crushed rock on the base, the position adjusting mechanism is connected with the microscope and used for adjusting the position of an objective lens of the microscope, and the picking mechanism is used for sucking elemental carbon particles.\|[0011] In some embodiments, the position adjustment mechanism includes montant, vertical sliding sleeve, vertical screw, horizontal sliding sleeve, horizontal pole, horizontal screw and support, the lower extreme of montant is fixed in the base, vertical sliding sleeve locates the montant to extend along vertical direction, set up first screw on the vertical sliding sleeve, vertical screw threaded connection in first screw, and be used for with montant butt, horizontal sliding sleeve is fixed in vertical sliding sleeve to extend along the horizontal direction, the horizontal pole slides and inserts and locate in the horizontal sliding sleeve, the second screw has been seted up on the horizontal sliding sleeve, horizontal screw threaded connection in the second screw, and be used for with the horizontal pole butt, the support is fixed in the one end of horizontal pole, the support with microscope fixed connection.\|[0012] In some embodiments, the support is provided with an inclined hole arranged obliquely, the sampling mechanism comprises a transparent pipe, a blocking net, a suction pump and a connecting hose, the transparent pipe is slidably inserted into the inclined hole, the lower end of the transparent pipe is used for absorbing simple substance carbon on the object placing plate, the blocking net is fixed at the lower end of the transparent pipe, and an inlet of the suction pump is communicated with the upper end of the transparent pipe through the connecting hose.\|[0013] In some embodiments, in the step S4, the crushed rock sample after removing the elemental carbon is burned in a high-temperature oxygen stream by a total organic carbon content detection device, and the content of the generated carbon dioxide is detected by an infrared detector, so as to obtain the total organic carbon content of the rock sample, where the total organic carbon content detection device includes a burner, an oxygen inlet mechanism, a buffer mechanism and the infrared detector;\| The burner comprises a burner body, a combustion table and an igniter, wherein a closed combustion cavity is formed in the burner body, an air inlet communicated with the combustion cavity is formed in one end of the burner body, an air outlet communicated with the combustion cavity is formed in the other end of the burner body, the combustion table is arranged in the burner body, and the igniter is arranged in the burner body; \| the oxygen inlet mechanism comprises an oxygen tank, an outlet valve, an air pump and an output pipe, the outlet valve is arranged at the outlet of the oxygen tank, the inlet of the air pump is communicated with the outlet valve, the outlet of the air pump is communicated with one end of the output pipe, the other end of the output pipe is communicated with the air inlet, and the output pipe is provided with the output valve; \| The buffer mechanism comprises a buffer tank and a vacuum pump, wherein a gas inlet is formed in one end of the buffer tank, a gas outlet is formed in the other end of the buffer tank, the gas inlet is communicated with the gas outlet through a conduit, a gas guide valve is arranged on the conduit, the inlet of the vacuum pump is communicated with the gas outlet through a gas exhaust pipe, and the gas exhaust pipe is provided with a gas exhaust valve; \| The infrared detector is arranged in the cache tank. \|[0014] In some embodiments, a one-way valve is also provided on the output tube.\|[0015] In some embodiments, the buffer tank is provided with a pressure detecting member thereon.\|[0016] Compared with the prior art, the method for measuring the total organic carbon content in the rock has the beneficial effects that: removing inorganic carbon in a sample through dilute hydrochloric acid, picking under a microscope to remove simple substance carbon in the crushed rock sample, burning the crushed rock sample after removing the simple substance carbon in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and obtaining the content of the total organic carbon through an infrared detector.\|DRAWINGS DESCRIPTION\|[0017] Fig. 1 is a schematic structural diagram of a method for measuring total organic carbon content in rock according to an embodiment of the present invention.\|[0018] Fig. 2 is a schematic structural view of the sample washing apparatus used in step S3 in fig. 1.\|[0019] Fig. 3 is a schematic structural diagram of a microscopic picking device used in step S4 in fig. 1.\|[0020] Fig. 4 is a partial enlarged view of the area a in fig. 3.\|[0021] FIG. 5 is a schematic view of the microscope sampling device of FIG. 3 when the transparent tube is lifted.\|[0022] Fig. 6 is a schematic view of the microscope sampling device of fig. 5 at another perspective.\|[0023] Fig. 7 is a schematic structural diagram of the total organic carbon content detecting device used in step S5 in fig. 1.\|[0024] The reference numerals are 100-sample cleaning device, 110-cylinder, 111-water outlet, 120-screen, 200-microscopic sample picking device, 210-base, 220-object placing plate, 230-microscope, 240-position adjusting mechanism, 241-vertical rod, 242-vertical sliding sleeve, 243-vertical screw, 244-horizontal sliding sleeve, 245-horizontal rod, 246-horizontal screw, 247-bracket, 250-sample picking mechanism, 251-transparent tube, 252-blocking net, 300-total organic carbon content detecting device, 310-burner, 311-furnace body, 312-combustion table, 313-igniter, 320-oxygen inlet mechanism, 321-oxygen tank, 322-outlet valve, 323-air pump, 324-output pipe, 325-output valve, 326-one-way valve, 330-buffering mechanism, 331-buffering tank, 3311-pressure detecting piece, 332-vacuum pump, 333-conduit, 334-air guide valve, 335-air suction tube, 336-suction valve, 340-infrared detector.\|INVENTION MODE\|Detailed Description\|[0025] The present invention will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0026] In order to solve the technical problem that the content of the measured total organic carbon is higher because simple substance carbon such as graphite and amorphous carbon possibly contained in a rock sample is not removed in the total organic carbon content measuring method, the invention provides the total organic carbon content measuring method in the rock, and the accuracy of measuring the total organic carbon content can be improved.\|[0027] Referring to fig. 1, fig. 1 is a flow chart of a method for determining total organic carbon content in rock according to an embodiment of the invention, the method for determining total organic carbon content in rock includes the following steps:\| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope to remove the simple substance carbon in the crushed rock sample, wherein the simple substance carbon in the rock is mainly graphite and amorphous carbon which are black, and the rock powder is usually light, so that the simple substance carbon can be easily identified and removed under the microscope; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|[0028] According to the technical scheme provided by the invention, after inorganic carbon in a sample is removed through dilute hydrochloric acid, sample picking is performed under a microscope to remove simple substance carbon in the rock fragments, then the rock fragments after simple substance carbon removal are combusted in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and the content of the total organic carbon is obtained through an infrared detector.\|[0029] In one embodiment, referring to fig. 1, in the step S1, the rock sample is ground to a particle size of less than 0.2mm, the mass of the ground sample is not less than 10g, and in the step S1, the mass of the weighed crushed rock sample is 0.01-1.00g, and is accurate to 0.0001g.\|[0030] In one embodiment, referring to fig.1, in the step S2, the container is placed in a water bath, the temperature of the water bath is controlled to be 60-80 ℃, and the sample is dissolved for more than 2 hours until the reaction is complete.\|[0031] In one embodiment, referring to fig. 1 and 2, in step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by the sample washing device 100, the sample washing device 100 includes a cylinder 110 and a screen 120, an upper end opening of the cylinder 110 is disposed, a water outlet 111 is disposed at a lower end of the cylinder 110, and the screen 120 is detachably mounted at the upper end opening of the cylinder 110. In use, the crushed rock sample after hydrochloric acid treatment is poured into the screen 120, and distilled water boiled is continuously introduced into the screen until the pH value of the crushed rock sample is neutral.\|[0032] In one embodiment, referring to fig. 1 and 3, in step S4, the cleaned crushed rock is picked by a microscopic picking device 200 to remove elemental carbon in the crushed rock, the microscopic picking device 200 includes a base 210, a placing plate 220, a microscope 230, a position adjusting mechanism 240, and a picking mechanism 250, the microscope 230 is located above the base 210, the placing plate 220 is used for placing the crushed rock on the base 210, the position adjusting mechanism 240 is connected with the microscope 230 and is used for adjusting the position of an objective lens of the microscope 230, and the picking mechanism 250 is used for sucking elemental carbon particles.\|[0033] In one embodiment, please refer to fig. 3-6, the position adjusting mechanism 240 includes a vertical rod 241, a vertical sliding sleeve 242, a vertical screw 243, a horizontal sliding sleeve 244, a cross rod 245, a horizontal screw 246 and a support 247, wherein the lower end of the vertical rod 241 is fixed in the base 210, the vertical sliding sleeve 242 is slidably sleeved on the vertical rod 241 and extends along the vertical direction, a first screw hole is formed in the vertical sliding sleeve 242, the vertical screw 243 is in threaded connection with the first screw hole and is used for being in butt joint with the vertical rod 241, the horizontal sliding sleeve 244 is fixed in the vertical sliding sleeve 242 and extends along the horizontal direction, the cross rod 245 is slidably inserted in the horizontal sliding sleeve 244, a second screw hole is formed in the horizontal sliding sleeve 244, the horizontal screw 246 is in threaded connection with the second screw hole and is used for being in butt joint with the cross rod 245, the support 247 is fixed at one end of the cross rod 245, the support 247 is fixedly connected with the microscope 230, and when in use, the vertical screw 243 is unscrewed, namely, the vertical sliding sleeve 242 is in threaded connection with the first screw hole, and is used for being in threaded connection with the vertical sliding sleeve 241, so as to enable the vertical sliding sleeve 241 to rotate around the microscope 241, thereby enable the vertical sliding sleeve 241 to rotate around the vertical rod 241, and the microscope 241 to reach the position of the microscope 230, and the position of the microscope 230 can be changed, and the position of the microscopic plate 220 can be different from the position of the microscopic plate 220, and the microscopic plate 220 can be in turn, or the position of the microscopic plate 220, and the position can be changed.\|[0034] In one embodiment, referring to fig. 3-6, the support 247 is provided with an inclined hole, the sample picking mechanism 250 includes a transparent tube 251, a blocking net 252, a suction pump (not shown) and a connection hose (not shown), the transparent tube 251 is slidably inserted into the inclined hole, the lower end of the transparent tube 251 is used for sucking the elemental carbon on the object placing plate 220, the blocking net 252 is fixed at the lower end of the transparent tube 251, the inlet of the suction pump is communicated with the upper end of the transparent tube 251 through the connection hose, when in use, the lower end of the transparent tube 251 is aligned with the elemental carbon, then the suction pump is started, the elemental carbon is sucked into the transparent tube 251 by the blocking net 252, then the transparent tube 251 is lifted, then the material receiving box is placed at the lower end of the transparent tube 251, then the suction pump is closed, and the elemental carbon in the transparent tube 251 falls into the material receiving box under the action of gravity, thereby removing the elemental carbon.\|[0035] In one embodiment, referring to fig. 1 and 7, in step S4, a crushed rock sample from which elemental carbon is removed is burned in a high-temperature oxygen stream by a total organic carbon content detection device 300, and the content of carbon dioxide generated is detected by an infrared detector to obtain the total organic carbon content of the rock sample, where the total organic carbon content detection device 300 includes a burner 310, an oxygen inlet mechanism 320, a buffer mechanism 330, and an infrared detector 340;\| the burner 310 comprises a burner body 311, a burner table 312 and an igniter 313, wherein a sealed combustion cavity is arranged in the burner body 311, an air inlet communicated with the combustion cavity is formed in one end of the burner body 311, an air outlet communicated with the combustion cavity is formed in the other end of the burner body 311, the burner table 312 is arranged in the burner body 311, and the igniter 313 is arranged in the burner body 311; \| The oxygen inlet mechanism 320 comprises an oxygen tank 321, an outlet valve 322, an air pump 323 and an output pipe 324, the outlet valve 322 is arranged at the outlet of the oxygen tank 321, the inlet of the air pump 323 is communicated with the outlet valve 322, the outlet of the air pump 323 is communicated with one end of the output pipe 324, the other end of the output pipe 324 is communicated with the air inlet, and the output pipe 324 is provided with an output valve 325; \| The buffer mechanism 330 comprises a buffer tank 331 and a vacuum pump 332, wherein a gas inlet is formed at one end of the buffer tank 331, a gas outlet is formed at the other end of the buffer tank 331, the gas inlet is communicated with the gas outlet through a conduit 333, a gas guide valve 334 is arranged on the conduit 333, an inlet of the vacuum pump 332 is communicated with the gas outlet through a gas exhaust pipe 335, and a gas exhaust valve 336 is arranged on the gas exhaust pipe 335; \| the infrared detector 340 is disposed in the buffer tank 331. \|[0036] The detection flow of the total organic carbon content detection device 300 is as follows:\| (1) Uniformly mixing the crushed rock sample after removing the simple substance carbon with the scrap iron cosolvent and the tungsten particle cosolvent, and placing the mixture in a combustion table 312; \| (2) Vacuumizing, closing the outlet valve 322, opening the output valve 325, the air guide valve 334 and the air extraction valve 336, and then opening the vacuum pump 332, wherein the vacuum pump vacuumizes the buffer tank 331, the oxygen tank 321 and the pipeline; \| (3) Oxygen is introduced, the air extraction valve 336 and the air guide valve 334 are closed, the outlet valve 322 is opened, and sufficient oxygen is introduced into the combustion chamber; \| (4) The igniter 313 ignites the sample on the combustion table 312, continuously introduces oxygen, and then opens the outlet valve 322 to introduce the generated gas into the buffer tank 331; \| (5) After full combustion, the output valve 325 is closed, combustion is stopped, after the system is stable, the carbon dioxide concentration in the buffer tank 331 is detected through the infrared detector 340, the carbon dioxide concentration in the buffer tank 331 is equal to the carbon dioxide concentration in the furnace body 311, the total amount of carbon dioxide generated by combustion can be obtained according to the carbon dioxide concentration multiplied by the total volume of the buffer tank 331, the furnace body 311 and the auxiliary pipeline, the total amount of organic carbon in the crushed rock sample is further obtained, and the total organic carbon content in the crushed rock sample can be obtained by dividing the total amount by the mass of the crushed rock sample. \|[0037] In one embodiment, referring to fig. 1 and 7, the output pipe 324 is further provided with a check valve 326, so as to avoid reverse flow of the gas.\|[0038] In one embodiment, referring to fig. 1 and 7, a pressure detecting member 3311 is provided on the buffer tank 331 to facilitate control of the reaction pressure.\|[0039] According to the technical scheme provided by the invention, after inorganic carbon in a sample is removed through dilute hydrochloric acid, sample picking is performed under a microscope to remove simple substance carbon in the rock fragments, then the rock fragments after simple substance carbon removal are combusted in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and the content of the total organic carbon is obtained through an infrared detector.\|[0040] The above-described embodiments of the present invention do not limit the scope of the present invention. Any other corresponding changes and modifications made in accordance with the technical idea of the present invention shall be included in the scope of the claims of the present invention.	Family Number\|(113895166)\|113895166\|Object of Invention\|(CN119666501 A)\|( . . . ) solution into the container , washing the rock fragments subjected to hydrochloric acid treatment to be neutral through distilled water , picking the washed rock fragments under a microscope , burning the rock fragments subjected to simple substance carbon removal in high - temperature oxygen flow , and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample . \|Abstract\|(CN119666501 A)\|The invention discloses a method for determining the total organic carbon content in rock , which comprises the following steps : grinding a rock sample , and weighing a preset mass of crushed rock sample ; putting the weighed crushed rock sample into a container , and adding an excessive hydrochloric acid solution into the container ; washing the crushed rock sample treated by hydrochloric acid with distilled water until the crushed rock sample is neutral ; picking the cleaned broken rock sample under a microscope ; burning the broken rock sample with the elemental carbon removed in high - temperature oxygen flow , and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample . The method has the beneficial effects that after inorganic carbon in the sample is removed through diluted hydrochloric acid , the sample is picked under a microscope , simple substance carbon in the crushed rock sample is removed , then the crushed rock sample with the simple substance carbon removed is combusted in high - temperature oxygen flow , the total organic carbon is converted into carbon dioxide , the content of the total organic carbon is obtained through an infrared detector , and the content of the total organic carbon in the crushed rock sample is calculated . And the accuracy of the total organic carbon content determination result can be improved . \|Independent Claims\|(CN119666501 A)\|( . . . ) S2 , placing the weighed crushed rock sample into a container , adding excessive hydrochloric acid solution into the container , and reacting to remove inorganic carbon in the crushed rock sample ; S3 , washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water ; S4 , picking the cleaned crushed rock sample under a microscope , and removing simple substance carbon in the crushed rock sample ; And S5 , burning the crushed rock sample with the elemental carbon removed in a high - temperature oxygen stream , and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample . \|	Measurement				G01N-001/28\|G01N-021/3504\|G01N-031/12	G01N-001/28\|G01N-021/3504\|G01N-031/12					CN118455193\|CN221516634U\|CN116884909\|CN219161963U\|CN215833688U\|CN113533619\|CN113030192\|CN110987767\|CN110044677\|CN107132098\|CN106442096\|CN104931310\|DE102012007348\|US20090078885	CN118455193 110987371 WHO=Examiner SELF=N CAT=A\|CN221516634U 111021276 WHO=Examiner SELF=N CAT=A\|CN116884909 106849386 WHO=Examiner SELF=N CAT=A\|CN219161963U 105258783 WHO=Examiner SELF=N CAT=A\|CN215833688U 98704829 WHO=Examiner SELF=N CAT=A\|CN113533619 96639665 WHO=Examiner SELF=N CAT=A\|CN113030192 94887941 WHO=Examiner SELF=N CAT=A\|CN110987767 88258761 WHO=Examiner SELF=N CAT=A\|CN110044677 85425821 WHO=Examiner SELF=N CAT=A\|CN107132098 77170469 WHO=Examiner SELF=N CAT=A\|CN106442096 75490447 WHO=Examiner SELF=N CAT=A\|CN104931310 70927439 WHO=Examiner SELF=N CAT=A\|DE102012007348 46165021 WHO=Examiner SELF=N CAT=A\|US20090078885 14120924 WHO=Examiner SELF=N CAT=A	浮爱青等: "沉积岩中总有机碳测定的方法验证", 《广州化学》, vol. 43, no. 05, 31 October 2018 (2018-10-31), pages 39 - 43 (Cat. Y,X)\|欧阳泉根等: "盐酸预处理-高频燃烧红外吸收法测定含铀岩石中有机碳", 《冶金分析》, vol. 40, no. 02, 29 February 2020 (2020-02-29), pages 18 - 23 (Cat. A)	CN104931310; CN106442096; CN107132098; CN110044677; CN113030192; CN113533619; CN215833688U; CN219161963U; CN116884909; CN221516634U; US20090078885; DE102012007348; CN110987767; CN118455193		PENDING	(CN119666501)\|PENDING	ALIVE	(CN119666501)\|ALIVE	(CN119666501)\|LEGAL DETAILS FOR CN119666501\|Actual or expected expiration date=2044-12-05\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-12-05\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202411779739\|Application date=2024-12-05\|Standardized application number=2024CN-1779739\|Event publication date=2025-03-21\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN119666501\|Publication stage code=A\|Publication date=2025-03-21\|Standardized publication number=CN119666501\|Event publication date=2025-03-21\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2025-04-08\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN119666501)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQRk0YvrOuH8Ffn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000076894002&ekey=2029&xpn=CN119666501&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=4oF3kmNZA1WO6CzMQqwYZpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN119666501)\|CN	(CN119666501)\|NAME=SHAANXI YANCHANG PETROLEUM (GROUP) CO. LTD. , COUNTRY=CN		(CN119666501)\|NAME=HE SHAN;XIAN YINUO PATENT AGENT CO. LTD. , REG=61220		(CN119666501)\|NAME=LIU SHUANGSHUANG\|NAME=CUI PENGXING\|NAME=LIU LILI\|NAME=KANG SHENGSONG\|NAME=ZHAO XUESI\|NAME=WANG TAO\|NAME=ZHU TONGTONG	(CN119666501)\|7	1	1					(CN119666501)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2025-03-21\|Gazette number: GAZNUM=41-1202\|Number of Pages: NPAGES=12\|		(CN119666501)\|CHINESE (CHI)	(CN119666501)\|Patent	Titre: (CN119666501)\|Method for determining total organic carbon content in rock Résumé: (CN119666501)\|The invention discloses a method for determining the total organic carbon content in rock, which comprises the following steps: grinding a rock sample, and weighing a preset mass of crushed rock sample; putting the weighed crushed rock sample into a container, and adding an excessive hydrochloric acid solution into the container; washing the crushed rock sample treated by hydrochloric acid with distilled water until the crushed rock sample is neutral; picking the cleaned broken rock sample under a microscope; burning the broken rock sample with the elemental carbon removed in high-temperature oxygen flow, and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample. The method has the beneficial effects that after inorganic carbon in the sample is removed through diluted hydrochloric acid, the sample is picked under a microscope, simple substance carbon in the crushed rock sample is removed, then the crushed rock sample with the simple substance carbon removed is combusted in high-temperature oxygen flow, the total organic carbon is converted into carbon dioxide, the content of the total organic carbon is obtained through an infrared detector, and the content of the total organic carbon in the crushed rock sample is calculated. And the accuracy of the total organic carbon content determination result can be improved.	12	Abstract	gpt-4o-mini	no	The article focuses on a method for determining total organic carbon content in rock, which does not relate to accelerated weathering or CO₂ capture.
15	GB202319995	WOGB2024/051780\|GB202319995	GB2636853\|WO2025/133560\|GB202319995	108540136	WO2025/133560 A1 2025-06-26 [WO2025133560]\|GB2636853 A 2025-07-02 [GB2636853]\|GB202319995 D0 2024-02-07 [GB202319995]	2023-12-22	2024-07-08\|2023-12-22	2025-07-02\|2025-06-26\|2024-02-07		(WO2025/133560)\|2027-06-22\|(GB2636853)\|2043-12-22	(WO2025/133560)\|Enhanced weathering carbon dioxide removal quantification method and apparatus	(WO2025/133560)\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water. Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal.	UNDO CARBON	(WO2025/133560)\|UNDO CARBON LTD ([GB])\|(GB2636853)\|Undo Carbon Ltd\|(GB202319995)\|Undo Carbon Ltd	LIU XINRAN	(WO2025/133560)\|LIU, Xinran	(WO2025/133560)\|BARNES IP LIMITED ([GB])	(WO2025/133560)\|However, when the soil has a low moisture content, it is difficult to extract enough moisture from the soil to get reliable data.\|Should the soil contain too little moisture, for example in circumstances where there has been little rainfall (e.g. when there has been a droughtfor a number of months), it becomes difficult to extract enough water from a soil sample to conduct normal tests of the pore water.\|	(WO2025/133560)\|1. A method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removing the soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850).\|	(WO2025/133560)\|According to a first aspect, there is provided method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removing the soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850).\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore soil water.\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water.\|	(WO2025/133560)\|SOIL SAMPLE(100,77)\|CARBON DIOXIDE(100,18)\|ENHANCED WEATHERING(100,11)\|PORE WATER SAMPLE(100,5)\|ENHANCED WEATHERING CARBON DIOXIDE(100,2)\|REMOVAL QUANTIFICATION(100,2)\|ENHANCED WEATHERING PRODUCT(67,2)\|ACIDIFIED DRIED SOIL SAMPLE(64,6)\|GROUND(61,39)\|MOISTURE CONTENT(55,6)\|CARBON DIOXIDE REMOVAL(50,4)\|ENOUGH MOISTURE(50,1)\|DROUGHT(46,1)\|CENTRIFUGE SPENT CORE SOLUTION(45,2)\|RAINFALL(44,2)\|PORE WATER EXTRACTION(40,2)\|PORE SOIL WATER(38,1)\|TREATED DRIED SOIL SAMPLE(36,4)\|RELIABLE DATA(36,1)\|STERILIZED DISTILLED WATER BATH(33,3)\|FACTOR CHANGE(30,2)\|DRAINAGE(28,2)\|AMMONIUM ACETATE SOLUTION(26,6)\|MONTH NUMBER(26,1)\|ENHANCED WEATHERING OPERATION(25,5)\|ARTIFICIAL RAIN WATER(24,3)\|GRAVEL(19,11)\|WATER CONTENT(18,5)\|OVEN(18,3)\|PORE WATER(17,10)\|ULTRAHIGH PURITY WATER(17,3)\|CRUSHED ROCK GEOCHEMICAL(16,1)\|SOIL CORE SAMPLE CONTAINER(14,6)\|MOISTURE PROBE(14,2)\|NITRIC ACID(14,2)\|MACRO RHYZON(14,1)\|EXTRACTING WATER CONTENT(12,3)\|ENHANCING SOIL(11,2)\|FARM MACHINERY(10,3)\|ANALYTICAL GRADE AMMONIUM ACETATE(10,1)\|ANALYTICAL GRADE AMMONIUM HYDROXIDE(10,1)\|MEASUREMENT OPTION(10,1)\|ROCK PARTICLE(10,1)\|TOTAL CATION QUANTIFICATION(10,1)\|TREATED SPENT CORE(10,1)\|RPM(9,4)\|SEA(9,3)\|BICARBONATE(8,2)\|CARBON DIOXIDE CAPTURE(8,2)\|TRAILER(8,2)\|ANALYTICAL GRADE ACETIC ACID(8,1)\|CATION CONTENT(8,1)\|CENTRIFUGE EQUIPMENT(8,1)\|DISPERSION(8,1)\|ENHANCED WEATHERING OPERATOR(8,1)\|MODELED CARBON CAPTURE(8,1)\|PARAMETER CALCULATION(8,1)\|SAMPLE DRY LAND(8,1)\|SPREADING CRUSHED SILICATE(8,1)\|STANDARD CENTRIFUGE(8,1)\|ULTRA HIGH PURITY WATER(8,1)\|BOTTOM LID(6,3)\|ADDING CRUSHED ROCK(6,1)\|ALKALINITY(6,1)\|BASALT(6,1)\|CENTRIFUGATION(6,1)\|ENHANCED WEATHERING PERFORMANCE(6,1)\|ENHANCED WEATHERING REACTION(6,1)\|FASTENING(6,1)\|LABORATORY(6,1)\|\|(GB2636853)\|SOIL SAMPLE(100,58)\|CARBON DIOXIDE(100,15)\|ENHANCED WEATHERING(100,9)\|PORE WATER SAMPLE(100,4)\|ENHANCED WEATHERING CARBON DIOXIDE(100,1)\|REMOVAL QUANTIFICATION(100,1)\|ENOUGH MOISTURE(38,1)\|GROUND(36,31)\|DROUGHT(35,1)\|RAINFALL(33,2)\|ENHANCED WEATHERING PRODUCT(32,1)\|MOISTURE CONTENT(30,5)\|PORE SOIL WATER(29,1)\|RELIABLE DATA(27,1)\|STERILIZED DISTILLED WATER BATH(25,3)\|DRAINAGE(21,2)\|MONTH NUMBER(20,1)\|CARBON DIOXIDE REMOVAL(19,2)\|ARTIFICIAL RAIN WATER(18,3)\|GRAVEL(14,11)\|WATER CONTENT(13,5)\|CRUSHED ROCK GEOCHEMICAL(12,1)\|ENHANCED WEATHERING OPERATION(10,4)\|MOISTURE PROBE(10,2)\|MACRO RHYZON(10,1)\|PORE WATER(9,9)\|EXTRACTING WATER CONTENT(9,3)\|FARM MACHINERY(7,3)\|SEA(7,3)\|MEASUREMENT OPTION(7,1)\|ROCK PARTICLE(7,1)\|BICARBONATE(6,2)\|CARBON DIOXIDE CAPTURE(6,2)\|TRAILER(6,2)\|1M HCL(6,1)\|CATION CONTENT(6,1)\|CENTRIFUGE EQUIPMENT(6,1)\|DISPERSION(6,1)\|ENHANCED WEATHERING OPERATOR(6,1)\|ENHANCING SOIL(6,1)\|MODELED CARBON CAPTURE(6,1)\|PARAMETER CALCULATION(6,1)\|SAMPLE DRY LAND(6,1)\|SPREADING CRUSHED SILICATE(6,1)\|STANDARD CENTRIFUGE(6,1)\|BOTTOM LID(5,3)\|ADDING CRUSHED ROCK(4,1)\|ALKALINITY(4,1)\|BASALT(4,1)\|ENHANCED WEATHERING PERFORMANCE(4,1)\|ENHANCED WEATHERING REACTION(4,1)\|FASTENING(4,1)\|LABORATORY(4,1)\|NEIGHBORING WATER MOLECULE(4,1)\|OUTGASSING(4,1)\|QUANTIFICATION(4,1)\|	(WO2025/133560)\|CLAIMS: \|1. A method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removing the soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850).\|2. The method of any preceding claim, wherein the soil sample is contained in a sample tube.\|3. The method of claim 2 wherein the sample tube is substantially made from metal and/or is substantially cylindrical.\|4. The method of either claims 2 or 3 wherein the sample tube comprises one or more caps, the one or more caps operable to seal the contents of the sample tube.\|5. The method of any preceding claim, wherein the bath of water comprises a bath of sterilised distilled water.\|6. The method of any preceding claim, wherein the step of placing the soil sample in a bath of water comprising placing the soil sample in the bath of water for substantially 24 hours and/or at substantially 2 to 4 degrees Celsius.\|7. The method of any preceding claim, wherein the step of removing the soil sample from the bath of water comprising removing the soil sample from the bath of water for sufficient duration to allow free drainage.\|8. The method of any preceding claim, wherein the step of applying pressure to the soil sample comprises placing the soil sample in a centrifuge.\|9. The method of claim 8 wherein the centrifuge spins the soil sample for substantially 30 minutes and/or at substantially 1 ,000 revolutions per minute.\|10. The method of any preceding claim further comprising the step of filtering the extracted water content.\|11. The method of claim 10 wherein the step of filtering is performed for substantially 5 to 10 minutes.\|12. The method of any preceding claim further comprising: drying the soil sample to create a dried soil sample; combining the dried soil sample with an ammonium acetate solution to create a spent core solution; applying pressure to the spent core solution; filtering the spent core solution to remove a treated dried soil sample; further treating the treated dried soil sample with an acid to create an acidified dried soil sample; and analysing the acidified dried soil sample to determine a measurement of cations in the acidified dried soil sample.\|13. The method of claim 12 wherein drying the soil sample comprising drying the soil sample in an oven and optionally crushing and/or mixing and/or sieving the soil sample to create the dried soil sample.\|14. The method of claims 12 or 13 further comprising the step of placing the dried soil sample in a rotating shaking apparatus.\|15. The method of any of claims 12 to 14, wherein applying pressure to the spent core solution comprises using a centrifuge apparatus to centrifuge the spent core solution.\|16. The method of any of claims 12 to 15 wherein the acid is nitric acid.\|17. The method of any of claims 12 to 16 wherein the ammonium acetate solution comprises any combination of: ammonium acetate; ammonium hydroxide; and ultra- high purity water.	(WO2025/133560)\|[0001] ENHANCED WEATHERING CARBON DIOXIDE REMOVAL QUANTIFICATION METHOD AND APPARATUS \| [0002] Field \| [0003] The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore soil water. \| [0004] Background \| [0005] Enhanced weathering is the process of spreading suitable crushed silicate rock materials over suitable land, such as farmland. Suitable rock materials include rock such as basalt, which naturally reacts with dissolved carbon dioxide in the form of carbonic acid to remove the carbon dioxide from the environment. By crushing the rock, the crushed rock has a larger surface area per particle which speeds up the process of capturing carbon dioxide by increasing the reaction surface area. By spreading the rock over, for example, farmland, carbon dioxide can be captured over a large land surface. \| [0006] During enhanced weathering, it is important to measure the properties of the enhanced weathering reaction in order to measure the amount of carbon dioxide captured in the soil, rivers and eventually oceans. This data can be used to compare against modelled carbon capture, verify carbon credits, or plan further enhanced weathering based on weathering performance. \| [0007] To measure enhanced weathering, one of the measurement options is to extract pore water using a tool called a macro rhyzon in order to determine the level of carbon capture from the sample or samples is obtained. However, when the soil has a low moisture content, it is difficult to extract enough moisture from the soil to get reliable data. \| [0008] Summary of Invention \| [0009] Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. \| [0010] According to a first aspect, there is provided method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removingthe soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850). \| [0011] By allowing the soil sample to be placed in water, the soil sample can saturate with water and this can allow the subsequent removal of both the added water and the original water content for subsequent testing. This can allow the testing of water in a soil sample containing substantially too low a moisture content to provide sufficient water for normal pore water testing. \| [0012] Optionally, the soil sample is contained in a sample tube. Optionally, the sample tube is substantially made from metal and/or is substantially cylindrical. Optionally, the sample tube comprises one or more caps, the one or more caps operable to seal the contents of the sample tube. \| [0013] The soil sample can be contained in a variety of configurations of sample apparatus, but can typically be obtained using a configuration of sample apparatus that is operable to work with a standard centrifuge and/or standard configuration of mechanical pressure apparatus. \| [0014] Optionally, the bath of water comprises a bath of sterilised distilled water. \| [0015] In other embodiments, artificial rainwater can be used. Using sterilised distilled water and/or artificial rainwater can allow the extracted water content to retain substantially all of the properties desired to be measured. \| [0016] Optionally, the step of placing the soil sample in a bath of water comprising placing the soil sample in the bath of water for substantially 24 hours and/or at substantially 2 to 4 degrees Celsius. \| [0017] Placing the soil sample in a bath of water under substantially these conditions can allow the soil sample to saturate with the water contained in the bath and/or substantially not change the properties of the soil sample and/or its water content. \| [0018] Optionally, the step of removing the soil sample from the bath of water comprising removing the soil sample from the bath of water for sufficient duration to allow free drainage. \| [0019] Removing the soil sample from the bath of water can allow only water that has been absorbed by the soil sample to remain prior to further step of the process being performed. \| [0020] Optionally, the step of applying pressure to the soil sample comprises placing the soil sample in a centrifuge. \| [0021] Placing the soil sample in a centrifuge can remove the moisture content of the soil substantially quickly, and/or causes water molecules being removed from the soil sample during the centrifuge operation to pull neighbouring water molecules out of the soil sample. \| [0022] Optionally, the centrifuge spins the soil sample for substantially 30 minutes and/or at substantially 1 ,000 revolutions per minute.Using this configuration of centrifuge equipment can allow sufficient water to be removed from the soil sample to allow subsequent tests to be performed on a substantially sufficient sample size. \| [0023] Optionally, the method further comprises the step of filtering the extracted water content. Optionally, the step of filtering is performed for substantially 5 to 10 minutes. \| [0024] By filtering the water, debris such as soil can be removed which might otherwise impact the measurements/analysis performed on the extracted water. \| [0025] Optionally, the method further comprises drying the soil sample to create a dried soil sample; combining the dried soil sample with an ammonium acetate solution to create a spent core solution; applying pressure to the spent core solution; filtering the spent core solution to remove a treated dried soil sample; further treating the treated dried soil sample with an acid to create an acidified dried soil sample; and analysing the acidified dried soil sample to determine a measurement of cations in the acidified dried soil sample. Optionally drying the soil sample comprising drying the soil sample in an oven and optionally crushing and/or mixing and/or sieving the soil sample to create the dried soil sample. Optionally, the method further comprises the step of placing the dried soil sample in a rotating shaking apparatus. Optionally applying pressure to the spent core solution comprises using a centrifuge apparatus to centrifuge the spent core solution. Optionally the acid is nitric acid. Optionally, the ammonium acetate solution comprises any combination of: ammonium acetate; ammonium hydroxide; and ultra-high purity water. \| [0026] By treating the “spent core” samples using ammonium acetate solution and analysing the treated spent cores, it is possible to measure the cations in the spent core and therefore at the site from which the core was obtained. \| [0027] Brief Description of Drawings \| [0028] Embodiments will now be described, by way of example only and with reference to the accompanying drawings having like-reference numerals, in which: \| [0029] Figure 1 shows an example enhanced weathering process; \| [0030] Figure 2 shows an example of a soil core sample container; \| [0031] Figure 3 shows an example of the use of the soil core sample container, prior to insertion into the soil to be sampled; \| [0032] Figure 4 shows an example of the use of the soil core sample container to insert into the soil to be sampled; \| [0033] Figure 5 shows an example of the use of the soil core sample container being removed from the soil to be sampled;Figure 6 shows an example of the use of the soil core sample container to contain the soil to be sampled; \| [0034] Figure 7 shows an example of the use of the soil core sample container being secured for transport with the soil sample inside; and \| [0035] Figure 8 shows an embodiment of the enhanced soil core moisture process. \| [0036] Specific Description \| [0037] Referring to Figure 1 , an example of an enhanced weathering process 100 will now be described. \| [0038] Enhanced weathering is performed by adding crushed rock 130 to farmland 140. In this described embodiment, the crushed rock 130 is added using farm machinery 120 such as a tractor with a trailer containing the crushed rock 130, where the trailer is configured to disperse the crushed rock 130 in a predetermined dispersal rate over substantially all of the surface of the farmland 140 as the farm machinery 120 travels along the farmland 140, typically travelling along parallel lines back and forth along the farmland 140. \| [0039] Not all of the land needs to be subject to enhanced weathering, so in this embodiment farmland 140 undergoes the enhanced weathering process 100 but non-weathered land 110 does not have any crushed rock 130 spread over its surface. \| [0040] In this embodiment, the properties of the farmland 140 that is to be subject to the enhanced weathering process 100 are determined in advance based on a combination of data for the area in which the farmland 140 is located along with data collected from the farmland 140. This data includes expected rainfall, pH, soil composition. Other data that is used as part of the process 100 is data pertaining to the crushed rock 130, including geochemical properties of the crushed rock and the range of surface area of the rock particles. Using this data, the amount of crushed rock 130 to spread over the farmland 140 and the density of spread/amount to be spread over the farmland 140 is calculated in advance of the spreading operation by the farm machinery 120. \| [0041] In other embodiments, different data can be obtained in advance of the spreading operation. In other embodiments, a spreading plan can comprise different arrangements for different parts of the farmland 140, for example differing amounts of rock to be spread on different portions of the farmland 140. In other embodiments, different equipment can be used to spread the crushed rock 130. In other embodiments, multiple spreading operations may be performed at one or more time intervals. In other embodiments, sensors can be used to monitor the properties of the farmland 140, before and/or after the one or more spreading operations being performed.Following the enhanced weathering operation 100, carbon dioxide is absorbed from the atmosphere above the farmland 140 by a chemical reaction between the dissolved carbon dioxide and the crushed rock 130 spread over the surface of the farmland 140. This captures and sequesters carbon dioxide from the atmosphere into the soil over substantially the entire area that has been subject to enhanced weathering operations 100. Depending on the parameters that have been calculated for the rock spreading operation(s), the rate of carbon dioxide capture depends on the amount and properties of the crushed rock 130 that has been spread over the farmland 140 and a prediction for this carbon dioxide capture will be determined from the calculated parameters for the rock spreading operation(s). \| [0042] Following the enhanced weathering operation 100, one of the measurements that needs to be performed to verify the amount of carbon captured is to measure the properties of the water in the soil, specifically the pore water. Pore water measurements can be key to understanding the soil chemistry and therefore how much carbon dioxide has been removed from the atmosphere. Enhanced weathering performance can depend on the pore water leaving the soil via the normal channels (e.g. streams and rivers) and reaching the ocean. Therefore, operators of enhanced weathering processes typically measure the contents of water in fields undergoing enhanced weathering to demonstrate bicarbonate and cation content in the pore water, which then leaves the soil and in time enters the ocean. \| [0043] Should the soil contain too little moisture, for example in circumstances where there has been little rainfall (e.g. when there has been a droughtfor a number of months), it becomes difficult to extract enough water from a soil sample to conduct normal tests of the pore water. If this is the case then the following process can be used to obtain sufficient water from soil that contains too little moisture. \| [0044] Pore water samples also should be analysed within around 36 hours of taking the sample, as the partial pressure of carbon dioxide in soil is different to that in air, so over time there is outgassing and degradation of the data (e.g. the bicarbonates in the soil sample will typically degrade over time as the pressure equilibrium moves from that of soil to that of air) that can be obtained from the pore water if tests aren’t performed promptly. \| [0045] Simply applying a large degree of pressure to the soil samples may not be possible is the moisture content is too low, as there is a limit to the amount of mechanical suction/pressure that is possible and depending on the type of soil it becomes impossible to extract sufficient water once the moisture levels drop below a certain level (this level varies by soil composition). Some methods of suction/pressure can extract sufficient water from soil samples but take too long, and after 36 hours from taking the soil sample the water extracted doesn’t provide a representative sample for analysis. \| [0046] Referring to Figure 2, an example soil core sample container 200 will now be described.The sample tube 220 is a hollow metal cylinder, which has two caps or lids, a top lid 210 and a bottom lid 230. The top and bottom lids 210, 230 are designed to fit on to the open ends of the tube 220 to secure and seal the sample soil contained within the sample tube 220. In this embodiment the caps 210, 230 fit to the ends of the tube 220 by an interference fit. In other embodiments, the caps 210, 230 can use a screw thread to fit to the tube 220. In other embodiments, other fixing mechanisms can be used to secure the lids 210, 230 to the tube 220. In this embodiment, each cylinder has a 5cm diameter and is 5cm deep. \| [0047] Typically, in this embodiment, multiple samples will be taken each with separate soil core sample containers, commensurate to the area of land being sampled. \| [0048] Referring to Figure 3, an example of use 300 of the soil core container of Figure 2 will now be described. \| [0049] A sample tube 310 (as described above in relation to Figure 2) is shown in this embodiment without caps. It is positioned above the surface of the soil 320. The intention is to sample a core of soil by inserting the sample tube 310 into the soil surface 320 to obtain a core of soil within the sample tube 310. \| [0050] Referring to Figure 4, an example of soil sampling 400 using the soil core container of Figure 2 will now be described. \| [0051] The sample tube 410 is inserted 440 into the soil, penetrating the soil surface 420 and thereby causing a sample of soil 430 to enter into the sample tube 410. In this embodiment, the tube 410 is hammered into the soil. \| [0052] Referring to Figure 5, an example of soil sample removal 500 using the soil core container of Figure 2 will now be described. \| [0053] The sample tube 510 is removed 540 from the soil surface 520, leaving a hole 550 and with the soil sample 530 contained within the sample tube 510. The soil sample 530 typically stays within the sample tube 510 when it is removed from the ground. It is typically very important to keep the soil core as a solid undisturbed soil sample hence it is kept intact within the cylinder 510. \| [0054] Referring to Figure 6, an example of securing the soil 600 within the soil core container of Figure 2 will now be described. \| [0055] The sample tube 610 containing the soil sample 630 then has the two lids 620, 640 placed at either open end of the cylinder 610 containing the soil sample 630. \| [0056] The top lid 620 is fit over one end of the sample tube 610 using an interference fit. The bottom lid 640 is fit over the other end of the sample tube 610 using an interference fit. The lids 620, 640 prevent the soil or any moisture from leaving the interior of the sample tube 610. \| [0057] In other embodiments, other fastening mechanisms can be used to fasten the lids 620, 640 to the tube 610.Referring to Figure 7, an example of readying the soil sample for transport 700 using the soil core container of Figure 2 will now be described. \| [0058] The sample tube 710 is shown with both lids 720, 740 securely fastened over either open end of the cylinder 710 containing the soil sample 730. The soil sample 730 is able to be transported securely within the sample tube 710, for example to a laboratory for testing the contents of the tube 710. \| [0059] Referring to Figure 8, an embodiment of the enhanced soil core moisture process 800 will now be described. \| [0060] In a first step 810, the soil sample in the sample tube is received 810. Typically this will be in a laboratory-setting with equipment to analyse the contents of the sample tube. \| [0061] In a second step 820, the soil sample tube has at least one lid removed and the open side of the tube is placed in a bath of sterilised distilled water. In this embodiment, each sample is saturated in 60ml of sterilised distilled water. \| [0062] In this embodiment, 60ml of sterilised distilled water should be sufficient for the soil sample size (using a 5cm diameter and 5cm deep cylinder) not to dilute the “signal” being analysed when testing the water extracted at the end of the process of this embodiment. \| [0063] In this embodiment, de-ionised water or very pure water is not used to prevent the soil leaching some of its contents into the bath of water (which will alter the subsequent analysis data detrimentally). In some embodiments, artificial rainwater can be used. \| [0064] In a third step 830, the sample tube is left for 24 hours at 2-4 degrees Celsius to saturate with the sterilised distilled water. \| [0065] In a fourth step 840, the sample tube is removed from the bath of water in order to allow free drainage of any water that hasn’t soaked into the soil sample in the tube. \| [0066] In a fifth step 850, the sample is placed into a centrifuge and spun for thirty minutes at 1 ,000 revolutions per minute in order to extract the water from the soil sample. The water is collected by the equipment. Typically about 20-30ml will be collected from each soil sample. \| [0067] In a sixth step 860, the water collected by the centrifuge is filtered for five to ten minutes. This filtered water can then be processed as would a normal pore water sample where the soil sample contains sufficient moisture. The filtration aims to remove for example small pieces of soil. In some embodiments, the filtration step could occur earlier by for example placing filter paper at at least one (or both) sides of the cylinder containing the soil sample. \| [0068] Measurements in this embodiment are then taken of alkalinity, pH and EC. In some embodiments, any or any combination of the following measurements as follows can be taken: pH using a benchtop pH meter; EC using a benchtop EC meter; alkalinity using titration using 0.1 M HCL; cations using ICP-AES; anions using IC. \| [0069] After centrifugation and pore water extraction, the core/soil samples are considered ‘spent’. Optionally, in some embodiments, the 'spent cores' are then slowly air dried in an ovenbefore being crushed, mixed and sieved in preparation for an ammonium acetate leach. In an embodiment, 2g of the dried soil is combined with ammonium acetate solution (in this embodiment, analytical grade NH4OAc ammonium acetate is used, with a formula weight of 77.08g/mol) before being placed into a rotating shaker for 2 hours at room temperature. The sample is then centrifuged in either 15ml or 50ml centrifuge tubes for 10 minutes at 4000 RPM before being allowed to settle for 10 mins. The solution is extracted and filtered before being acidified with nitric acid (in this embodiment, analytical grade HNO3 nitric acid, with a formula weight of 63.01 g/mol, is used). The filtered and acidified solution is sent to analysis by ICP- MS. This method allows a quantification of total cations held on the soil exchange sites. \| [0070] In the example embodiment, the ammonium acetate solution comprises a mixture of analytical grade ammonium acetate (NH4OAc; Formula weight = 77.08 g/mol); analytical grade ammonium hydroxide (NH4OH; Formula weight = 35.04 g/mol); analytical grade acetic acid (CH3COOH; Formula weight = 60.05 g/mol); and ultra-high purity water. The ammonium acetate and ultra-high purity water are mixed first, to create a 1M solution. The pH of the solution is then measured in order to then adjust the pH of the solution to pH8.5, by either adding acetic acid to lower the pH or by adding ammonium hydroxide to raise the pH of the solution. \| [0071] In some embodiments, a moisture probe can be used in the soil to be sample prior to take soil core samples and the data from the moisture probe can be used to determine how much water should be contained in the water bath in order to determine how much the pore water sample is diluted by the saturation step in process 800. \| [0072] In some embodiments, in place of a centrifuge, a mechanical pressure device can be used such as a hydraulic press. \| [0073] Any system feature as described herein may also be provided as a method feature, and vice versa. As used herein, means plus function features may be expressed alternatively in terms of their corresponding structure. \| [0074] Any feature in one aspect may be applied to other aspects, in any appropriate combination. In particular, method aspects may be applied to system aspects, and vice versa. Furthermore, any, some and/or all features in one aspect can be applied to any, some and/or all features in any other aspect, in any appropriate combination. \| [0075] It should also be appreciated that particular combinations of the various features described and defined in any aspects can be implemented and/or supplied and/or used independently.	(WO2025/133560)\|[0001] ENHANCED WEATHERING CARBON DIOXIDE REMOVAL QUANTIFICATION METHOD AND APPARATUS \| [0002] Field \| [0003] The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore soil water. \| [0004] Background \| [0005] Enhanced weathering is the process of spreading suitable crushed silicate rock materials over suitable land, such as farmland. Suitable rock materials include rock such as basalt, which naturally reacts with dissolved carbon dioxide in the form of carbonic acid to remove the carbon dioxide from the environment. By crushing the rock, the crushed rock has a larger surface area per particle which speeds up the process of capturing carbon dioxide by increasing the reaction surface area. By spreading the rock over, for example, farmland, carbon dioxide can be captured over a large land surface. \| [0006] During enhanced weathering, it is important to measure the properties of the enhanced weathering reaction in order to measure the amount of carbon dioxide captured in the soil, rivers and eventually oceans. This data can be used to compare against modelled carbon capture, verify carbon credits, or plan further enhanced weathering based on weathering performance. \| [0007] To measure enhanced weathering, one of the measurement options is to extract pore water using a tool called a macro rhyzon in order to determine the level of carbon capture from the sample or samples is obtained. However, when the soil has a low moisture content, it is difficult to extract enough moisture from the soil to get reliable data. \| [0008] Summary of Invention \| [0009] Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. \| [0010] According to a first aspect, there is provided method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removingthe soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850). \| [0011] By allowing the soil sample to be placed in water, the soil sample can saturate with water and this can allow the subsequent removal of both the added water and the original water content for subsequent testing. This can allow the testing of water in a soil sample containing substantially too low a moisture content to provide sufficient water for normal pore water testing. \| [0012] Optionally, the soil sample is contained in a sample tube. Optionally, the sample tube is substantially made from metal and/or is substantially cylindrical. Optionally, the sample tube comprises one or more caps, the one or more caps operable to seal the contents of the sample tube. \| [0013] The soil sample can be contained in a variety of configurations of sample apparatus, but can typically be obtained using a configuration of sample apparatus that is operable to work with a standard centrifuge and/or standard configuration of mechanical pressure apparatus. \| [0014] Optionally, the bath of water comprises a bath of sterilised distilled water. \| [0015] In other embodiments, artificial rainwater can be used. Using sterilised distilled water and/or artificial rainwater can allow the extracted water content to retain substantially all of the properties desired to be measured. \| [0016] Optionally, the step of placing the soil sample in a bath of water comprising placing the soil sample in the bath of water for substantially 24 hours and/or at substantially 2 to 4 degrees Celsius. \| [0017] Placing the soil sample in a bath of water under substantially these conditions can allow the soil sample to saturate with the water contained in the bath and/or substantially not change the properties of the soil sample and/or its water content. \| [0018] Optionally, the step of removing the soil sample from the bath of water comprising removing the soil sample from the bath of water for sufficient duration to allow free drainage. \| [0019] Removing the soil sample from the bath of water can allow only water that has been absorbed by the soil sample to remain prior to further step of the process being performed. \| [0020] Optionally, the step of applying pressure to the soil sample comprises placing the soil sample in a centrifuge. \| [0021] Placing the soil sample in a centrifuge can remove the moisture content of the soil substantially quickly, and/or causes water molecules being removed from the soil sample during the centrifuge operation to pull neighbouring water molecules out of the soil sample. \| [0022] Optionally, the centrifuge spins the soil sample for substantially 30 minutes and/or at substantially 1 ,000 revolutions per minute.Using this configuration of centrifuge equipment can allow sufficient water to be removed from the soil sample to allow subsequent tests to be performed on a substantially sufficient sample size. \| [0023] Optionally, the method further comprises the step of filtering the extracted water content. Optionally, the step of filtering is performed for substantially 5 to 10 minutes. \| [0024] By filtering the water, debris such as soil can be removed which might otherwise impact the measurements/analysis performed on the extracted water. \| [0025] Optionally, the method further comprises drying the soil sample to create a dried soil sample; combining the dried soil sample with an ammonium acetate solution to create a spent core solution; applying pressure to the spent core solution; filtering the spent core solution to remove a treated dried soil sample; further treating the treated dried soil sample with an acid to create an acidified dried soil sample; and analysing the acidified dried soil sample to determine a measurement of cations in the acidified dried soil sample. Optionally drying the soil sample comprising drying the soil sample in an oven and optionally crushing and/or mixing and/or sieving the soil sample to create the dried soil sample. Optionally, the method further comprises the step of placing the dried soil sample in a rotating shaking apparatus. Optionally applying pressure to the spent core solution comprises using a centrifuge apparatus to centrifuge the spent core solution. Optionally the acid is nitric acid. Optionally, the ammonium acetate solution comprises any combination of: ammonium acetate; ammonium hydroxide; and ultra-high purity water. \| [0026] By treating the “spent core” samples using ammonium acetate solution and analysing the treated spent cores, it is possible to measure the cations in the spent core and therefore at the site from which the core was obtained. \| [0027] Brief Description of Drawings \| [0028] Embodiments will now be described, by way of example only and with reference to the accompanying drawings having like-reference numerals, in which: \| [0029] Figure 1 shows an example enhanced weathering process; \| [0030] Figure 2 shows an example of a soil core sample container; \| [0031] Figure 3 shows an example of the use of the soil core sample container, prior to insertion into the soil to be sampled; \| [0032] Figure 4 shows an example of the use of the soil core sample container to insert into the soil to be sampled; \| [0033] Figure 5 shows an example of the use of the soil core sample container being removed from the soil to be sampled;Figure 6 shows an example of the use of the soil core sample container to contain the soil to be sampled; \| [0034] Figure 7 shows an example of the use of the soil core sample container being secured for transport with the soil sample inside; and \| [0035] Figure 8 shows an embodiment of the enhanced soil core moisture process. \| [0036] Specific Description \| [0037] Referring to Figure 1 , an example of an enhanced weathering process 100 will now be described. \| [0038] Enhanced weathering is performed by adding crushed rock 130 to farmland 140. In this described embodiment, the crushed rock 130 is added using farm machinery 120 such as a tractor with a trailer containing the crushed rock 130, where the trailer is configured to disperse the crushed rock 130 in a predetermined dispersal rate over substantially all of the surface of the farmland 140 as the farm machinery 120 travels along the farmland 140, typically travelling along parallel lines back and forth along the farmland 140. \| [0039] Not all of the land needs to be subject to enhanced weathering, so in this embodiment farmland 140 undergoes the enhanced weathering process 100 but non-weathered land 110 does not have any crushed rock 130 spread over its surface. \| [0040] In this embodiment, the properties of the farmland 140 that is to be subject to the enhanced weathering process 100 are determined in advance based on a combination of data for the area in which the farmland 140 is located along with data collected from the farmland 140. This data includes expected rainfall, pH, soil composition. Other data that is used as part of the process 100 is data pertaining to the crushed rock 130, including geochemical properties of the crushed rock and the range of surface area of the rock particles. Using this data, the amount of crushed rock 130 to spread over the farmland 140 and the density of spread/amount to be spread over the farmland 140 is calculated in advance of the spreading operation by the farm machinery 120. \| [0041] In other embodiments, different data can be obtained in advance of the spreading operation. In other embodiments, a spreading plan can comprise different arrangements for different parts of the farmland 140, for example differing amounts of rock to be spread on different portions of the farmland 140. In other embodiments, different equipment can be used to spread the crushed rock 130. In other embodiments, multiple spreading operations may be performed at one or more time intervals. In other embodiments, sensors can be used to monitor the properties of the farmland 140, before and/or after the one or more spreading operations being performed.Following the enhanced weathering operation 100, carbon dioxide is absorbed from the atmosphere above the farmland 140 by a chemical reaction between the dissolved carbon dioxide and the crushed rock 130 spread over the surface of the farmland 140. This captures and sequesters carbon dioxide from the atmosphere into the soil over substantially the entire area that has been subject to enhanced weathering operations 100. Depending on the parameters that have been calculated for the rock spreading operation(s), the rate of carbon dioxide capture depends on the amount and properties of the crushed rock 130 that has been spread over the farmland 140 and a prediction for this carbon dioxide capture will be determined from the calculated parameters for the rock spreading operation(s). \| [0042] Following the enhanced weathering operation 100, one of the measurements that needs to be performed to verify the amount of carbon captured is to measure the properties of the water in the soil, specifically the pore water. Pore water measurements can be key to understanding the soil chemistry and therefore how much carbon dioxide has been removed from the atmosphere. Enhanced weathering performance can depend on the pore water leaving the soil via the normal channels (e.g. streams and rivers) and reaching the ocean. Therefore, operators of enhanced weathering processes typically measure the contents of water in fields undergoing enhanced weathering to demonstrate bicarbonate and cation content in the pore water, which then leaves the soil and in time enters the ocean. \| [0043] Should the soil contain too little moisture, for example in circumstances where there has been little rainfall (e.g. when there has been a droughtfor a number of months), it becomes difficult to extract enough water from a soil sample to conduct normal tests of the pore water. If this is the case then the following process can be used to obtain sufficient water from soil that contains too little moisture. \| [0044] Pore water samples also should be analysed within around 36 hours of taking the sample, as the partial pressure of carbon dioxide in soil is different to that in air, so over time there is outgassing and degradation of the data (e.g. the bicarbonates in the soil sample will typically degrade over time as the pressure equilibrium moves from that of soil to that of air) that can be obtained from the pore water if tests aren’t performed promptly. \| [0045] Simply applying a large degree of pressure to the soil samples may not be possible is the moisture content is too low, as there is a limit to the amount of mechanical suction/pressure that is possible and depending on the type of soil it becomes impossible to extract sufficient water once the moisture levels drop below a certain level (this level varies by soil composition). Some methods of suction/pressure can extract sufficient water from soil samples but take too long, and after 36 hours from taking the soil sample the water extracted doesn’t provide a representative sample for analysis. \| [0046] Referring to Figure 2, an example soil core sample container 200 will now be described.The sample tube 220 is a hollow metal cylinder, which has two caps or lids, a top lid 210 and a bottom lid 230. The top and bottom lids 210, 230 are designed to fit on to the open ends of the tube 220 to secure and seal the sample soil contained within the sample tube 220. In this embodiment the caps 210, 230 fit to the ends of the tube 220 by an interference fit. In other embodiments, the caps 210, 230 can use a screw thread to fit to the tube 220. In other embodiments, other fixing mechanisms can be used to secure the lids 210, 230 to the tube 220. In this embodiment, each cylinder has a 5cm diameter and is 5cm deep. \| [0047] Typically, in this embodiment, multiple samples will be taken each with separate soil core sample containers, commensurate to the area of land being sampled. \| [0048] Referring to Figure 3, an example of use 300 of the soil core container of Figure 2 will now be described. \| [0049] A sample tube 310 (as described above in relation to Figure 2) is shown in this embodiment without caps. It is positioned above the surface of the soil 320. The intention is to sample a core of soil by inserting the sample tube 310 into the soil surface 320 to obtain a core of soil within the sample tube 310. \| [0050] Referring to Figure 4, an example of soil sampling 400 using the soil core container of Figure 2 will now be described. \| [0051] The sample tube 410 is inserted 440 into the soil, penetrating the soil surface 420 and thereby causing a sample of soil 430 to enter into the sample tube 410. In this embodiment, the tube 410 is hammered into the soil. \| [0052] Referring to Figure 5, an example of soil sample removal 500 using the soil core container of Figure 2 will now be described. \| [0053] The sample tube 510 is removed 540 from the soil surface 520, leaving a hole 550 and with the soil sample 530 contained within the sample tube 510. The soil sample 530 typically stays within the sample tube 510 when it is removed from the ground. It is typically very important to keep the soil core as a solid undisturbed soil sample hence it is kept intact within the cylinder 510. \| [0054] Referring to Figure 6, an example of securing the soil 600 within the soil core container of Figure 2 will now be described. \| [0055] The sample tube 610 containing the soil sample 630 then has the two lids 620, 640 placed at either open end of the cylinder 610 containing the soil sample 630. \| [0056] The top lid 620 is fit over one end of the sample tube 610 using an interference fit. The bottom lid 640 is fit over the other end of the sample tube 610 using an interference fit. The lids 620, 640 prevent the soil or any moisture from leaving the interior of the sample tube 610. \| [0057] In other embodiments, other fastening mechanisms can be used to fasten the lids 620, 640 to the tube 610.Referring to Figure 7, an example of readying the soil sample for transport 700 using the soil core container of Figure 2 will now be described. \| [0058] The sample tube 710 is shown with both lids 720, 740 securely fastened over either open end of the cylinder 710 containing the soil sample 730. The soil sample 730 is able to be transported securely within the sample tube 710, for example to a laboratory for testing the contents of the tube 710. \| [0059] Referring to Figure 8, an embodiment of the enhanced soil core moisture process 800 will now be described. \| [0060] In a first step 810, the soil sample in the sample tube is received 810. Typically this will be in a laboratory-setting with equipment to analyse the contents of the sample tube. \| [0061] In a second step 820, the soil sample tube has at least one lid removed and the open side of the tube is placed in a bath of sterilised distilled water. In this embodiment, each sample is saturated in 60ml of sterilised distilled water. \| [0062] In this embodiment, 60ml of sterilised distilled water should be sufficient for the soil sample size (using a 5cm diameter and 5cm deep cylinder) not to dilute the “signal” being analysed when testing the water extracted at the end of the process of this embodiment. \| [0063] In this embodiment, de-ionised water or very pure water is not used to prevent the soil leaching some of its contents into the bath of water (which will alter the subsequent analysis data detrimentally). In some embodiments, artificial rainwater can be used. \| [0064] In a third step 830, the sample tube is left for 24 hours at 2-4 degrees Celsius to saturate with the sterilised distilled water. \| [0065] In a fourth step 840, the sample tube is removed from the bath of water in order to allow free drainage of any water that hasn’t soaked into the soil sample in the tube. \| [0066] In a fifth step 850, the sample is placed into a centrifuge and spun for thirty minutes at 1 ,000 revolutions per minute in order to extract the water from the soil sample. The water is collected by the equipment. Typically about 20-30ml will be collected from each soil sample. \| [0067] In a sixth step 860, the water collected by the centrifuge is filtered for five to ten minutes. This filtered water can then be processed as would a normal pore water sample where the soil sample contains sufficient moisture. The filtration aims to remove for example small pieces of soil. In some embodiments, the filtration step could occur earlier by for example placing filter paper at at least one (or both) sides of the cylinder containing the soil sample. \| [0068] Measurements in this embodiment are then taken of alkalinity, pH and EC. In some embodiments, any or any combination of the following measurements as follows can be taken: pH using a benchtop pH meter; EC using a benchtop EC meter; alkalinity using titration using 0.1 M HCL; cations using ICP-AES; anions using IC. \| [0069] After centrifugation and pore water extraction, the core/soil samples are considered ‘spent’. Optionally, in some embodiments, the 'spent cores' are then slowly air dried in an ovenbefore being crushed, mixed and sieved in preparation for an ammonium acetate leach. In an embodiment, 2g of the dried soil is combined with ammonium acetate solution (in this embodiment, analytical grade NH4OAc ammonium acetate is used, with a formula weight of 77.08g/mol) before being placed into a rotating shaker for 2 hours at room temperature. The sample is then centrifuged in either 15ml or 50ml centrifuge tubes for 10 minutes at 4000 RPM before being allowed to settle for 10 mins. The solution is extracted and filtered before being acidified with nitric acid (in this embodiment, analytical grade HNO3 nitric acid, with a formula weight of 63.01 g/mol, is used). The filtered and acidified solution is sent to analysis by ICP- MS. This method allows a quantification of total cations held on the soil exchange sites. \| [0070] In the example embodiment, the ammonium acetate solution comprises a mixture of analytical grade ammonium acetate (NH4OAc; Formula weight = 77.08 g/mol); analytical grade ammonium hydroxide (NH4OH; Formula weight = 35.04 g/mol); analytical grade acetic acid (CH3COOH; Formula weight = 60.05 g/mol); and ultra-high purity water. The ammonium acetate and ultra-high purity water are mixed first, to create a 1M solution. The pH of the solution is then measured in order to then adjust the pH of the solution to pH8.5, by either adding acetic acid to lower the pH or by adding ammonium hydroxide to raise the pH of the solution. \| [0071] In some embodiments, a moisture probe can be used in the soil to be sample prior to take soil core samples and the data from the moisture probe can be used to determine how much water should be contained in the water bath in order to determine how much the pore water sample is diluted by the saturation step in process 800. \| [0072] In some embodiments, in place of a centrifuge, a mechanical pressure device can be used such as a hydraulic press. \| [0073] Any system feature as described herein may also be provided as a method feature, and vice versa. As used herein, means plus function features may be expressed alternatively in terms of their corresponding structure. \| [0074] Any feature in one aspect may be applied to other aspects, in any appropriate combination. In particular, method aspects may be applied to system aspects, and vice versa. Furthermore, any, some and/or all features in one aspect can be applied to any, some and/or all features in any other aspect, in any appropriate combination. \| [0075] It should also be appreciated that particular combinations of the various features described and defined in any aspects can be implemented and/or supplied and/or used independently.	Family Number\|(108540136)\|108540136\|Object of Invention\|(GB2636853 A)\|The present invention relates to methods of quantifying carbon dioxide removal when performing enhanced weathering operations. \|(WO2025133560 A1)\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. \|Abstract\|(GB2636853 A)\|A method for quantifying carbon dioxide removal when performing enhance weathering operations. Measurements are enabled by taking soil cores 810, placing the core sample into a water bath, 820, leave sample to saturate 830, drain sample 840, apply pressure on the sample 850 to allow a pore sample of water to be extracted from the soil sample 860. Filtering may be carried out on the pore water sample during collection. Thus, pore water samples may be extracted from soil that may not have enough moisture to extract a sufficiently large enough pore sample. The method may then be used to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. Enhanced weathering is a process of spreading suitable crushed silicate rock materials over land such as farmland enabling carbon dioxide to be captured over a large area.\|(WO2025133560 A1)\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water. Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal.\|Title\|(GB202319995 D0)\|Enhanced weathering carbon dioxide removal quantification method and apparatus\|(GB2636853 A)\|Enhanced weathering carbon dioxide removal quantification method and apparatus\|(WO2025133560 A1)\|Enhanced weathering carbon dioxide removal quantification method and apparatus\|	Analysis of biological materials	G01N-001/28\|G01N-033/24\|G01N-033/24/6		G01N-001/28\|G01N-033/24\|G01N-033/24/6	G01N-001/28\|G01N-033/24	G01N-001/28\|G01N-033/24					US20120103077\|CN115307977\|CN112525630\|CN203772616U	US20120103077 44414932 WHO=Examiner SELF=N CAT=A\|CN115307977 102493973 WHO=Examiner SELF=N\|CN112525630 93215294 WHO=Examiner SELF=N\|CN203772616U 67217407 WHO=Examiner SELF=N		XP091560179; XP086002247; US20120103077; XP037697290\|CN203772616U; CN115307977; CN112525630	(WO2025/133560)\|International Search Report [Examiner]\|-DAVID J BEERLING ET AL: "Enhanced weathering in the U.S. Corn Belt delivers carbon removal with agronomic benefits", ARXIV.ORG, CORNELL UNIVERSITY LIBRARY, 201 OLIN LIBRARY CORNELL UNIVERSITY ITHACA, NY 14853, 6 July 2023 (2023-07-06), XP091560179\|-LOZANO J C ET AL: "A system for obtaining soil solution extracts and soil water retention curves using a bench centrifuge with fixed angle rotors", GEODERMA, ELSEVIER, AMSTERDAM, NL, vol. 361, 27 November 2019 (2019-11-27), XP086002247, ISSN: 0016-7061, [retrieved on 20191127], DOI: 10.1016/J.GEODERMA.2019.114063\|-LAUKKANEN JOHANNA ET AL: "In situ remediation of metal(loid)-contaminated lake sediments with alkali-activated blast furnace slag granule amendment: A field experiment", JOURNAL OF SOILS AND SEDIMENTS, SPRINGER, DE, vol. 22, no. 3, 26 January 2022 (2022-01-26), pages 1054 - 1067, XP037697290, ISSN: 1439-0108, [retrieved on 20220126], DOI: 10.1007/S11368-022-03140-Z\|\|	PENDING	(WO2025/133560)\|PENDING\|(GB2636853)\|PENDING	ALIVE	(WO2025/133560)\|ALIVE\|(GB2636853)\|ALIVE	(WO2025/133560)\|LEGAL DETAILS FOR WO2025/133560\|Actual or expected expiration date=2027-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-07-08\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOGB2024/051780\|Application date=2024-07-08\|Standardized application number=2024WO-GB51780\|Event publication date=2025-06-26\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/133560\|Publication stage code=A1\|Publication date=2025-06-26\|Standardized publication number=WO2025133560\|Event publication date=2025-11-06\|Event code=WO/DPE1\|Event group=Examination events\|Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2044-07-08\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP24743471\|Event publication date=2025-08-06\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|(GB2636853)\|LEGAL DETAILS FOR GB2636853\|Actual or expected expiration date=2043-12-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-12-22\|Event code=GB/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=GB GB202319995\|Application date=2023-12-22\|Standardized application number=2023GB-0019995\|Event publication date=2024-02-07\|Event code=GB/D0\|Event indicator=Pos\|Event group=Examination events\|Patent application filed\|Publication country=GB\|Publication number=GB202319995\|Publication stage code=D0\|Publication date=2024-02-07\|Standardized publication number=GB202319995\|Event publication date=2025-07-02\|Event code=GB/A\|Event group=Examination events\|Published Application\|Publication country=GB\|Publication number=GB2636853\|Publication stage code=A\|Publication date=2025-07-02\|Standardized publication number=GB2636853	(WO2025/133560)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/133560)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/133560)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/133560)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/133560)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(WO2025/133560)\|WO; EP\|(GB2636853)\|GB	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=icjTorqguCAiwlzxUQ66p90P/F2Pwh1EkaV0SMUACwOCCKReMmHu7M9Ry4MrhQjLALkMBz8hwaI=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006802716&ekey=2486&xpn=WO2025133560&kind=A1	http://www.wipo.int/patentscope/search/en/detail.jsf?docId=WO2025133560&redirectedID=true	https://permalink.orbit.com/RenderStaticFirstPage?XPN=OThLP3Yvv2mkh5CpoqtjpbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	GB	(WO2025/133560)\|GB	(WO2025/133560)\|NAME=UNDO CARBON LTD 3rd Floor 86-90 Paul Street London, EC2A 4NE , COUNTRY=GB	(WO2025/133560)\|GB	(WO2025/133560)\|NAME=BARNES IP LIMITED Castle Hill House 12 Castle Hill Windsor Berkshire SL4 1PD , POSTCODE=SL4 1PD , COUNTRY=GB	(WO2025/133560)\|GB\|	(WO2025/133560)\|NAME=LIU, Xinran c/o Undo Carbon Ltd 3rd Floor 86-90 Paul Street London Greater London EC2A 4NE, POSTCODE=EC2A 4NE, COUNTRY=GB\|(GB2636853)\|NAME=Xinran Liu	(WO2025/133560)\|8\|(GB2636853)\|8	1	2					(WO2025/133560)\|Number of Claims: NCL=17\|Extended kind: EXTK=x\|\|(GB2636853)\|Number of Claims: NCL=11\|\|(GB202319995)\|Gazette date: GAZDATE=2024-02-07\|		(WO2025/133560)\|ENGLISH (ENG)	(GB2636853)\|Patent\|(WO2025133560)\|Patent\|(GB202319995)\|Patent	Titre: (WO2025/133560)\|Enhanced weathering carbon dioxide removal quantification method and apparatus Résumé: (WO2025/133560)\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water. Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal.	11	Abstract	gpt-4o-mini	yes	The article focuses on enhanced weathering methods for quantifying carbon dioxide removal, which is central to the topic of accelerated weathering and carbon sequestration.
16	AU2007900853	ZA200906476\|ZA200906474	ZA200906476\|ZA200906474	65403466	ZA200906476 B 2010-09-29 [ZA200906476]\|ZA200906474 B 2010-07-28 [ZA200906474]	2007-02-20	2009-09-17\|2009-09-17	2010-09-29\|2010-07-28	(ZA200906476)\|2010-09-29\|(ZA200906474)\|2010-07-28	(ZA200906476)\|2029-09-17\|(ZA200906474)\|2029-09-17	(ZA200906476)\|System, apparatus and method for carbon dioxide sequestration	(ZA200906476)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From CN101641145 A)	HUNWICK RICHARD J\|HUNWICK RICHARD J	(ZA200906476)\|HUNWICK, RICHARD J\|(ZA200906474)\|HUNWICK, RICHARD J	HUNWICK RICHARD J	(ZA200906476)\|HUNWICK, RICHARD J									Family Number\|(65403466)\|65403466\|Abstract\|(ZA200906474 B)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From CN101641145 A)\|(ZA200906476 B)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From CN101641145 A)\|Title\|(ZA200906474 B)\|System, apparatus and method for carbon dioxide sequestration\|(ZA200906476 B)\|System, apparatus and method for carbon dioxide sequestration\|	Chemical engineering\|Materials, metallurgy	Y02A-050/20\|Y02P-020/151		Y02A-050/20\|Y02P-020/151	B01D\|C01B\|C01B-032/50\|C01B-032/60	B01D\|C01B\|C01B-032/50\|C01B-032/60										GRANTED	(ZA200906476)\|GRANTED\|(ZA200906474)\|GRANTED	ALIVE	(ZA200906476)\|ALIVE\|(ZA200906474)\|ALIVE	(ZA200906476)\|LEGAL DETAILS FOR ZA200906476\|Actual or expected expiration date=2029-09-17\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2009-09-17\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA200906476\|Application date=2009-09-17\|Standardized application number=2009ZA-0006476\|Event publication date=2010-09-29\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA200906476\|Publication stage code=B\|Publication date=2010-09-29\|Standardized publication number=ZA200906476\|(ZA200906474)\|LEGAL DETAILS FOR ZA200906474\|Actual or expected expiration date=2029-09-17\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2009-09-17\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA200906474\|Application date=2009-09-17\|Standardized application number=2009ZA-0006474\|Event publication date=2010-07-28\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA200906474\|Publication stage code=B\|Publication date=2010-07-28\|Standardized publication number=ZA200906474		(ZA200906476)\|ZA\|(ZA200906474)\|ZA	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=U29pnpjL83VLPRBewy3fiKQ6hYovoTT3WeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1			https://permalink.orbit.com/RenderStaticFirstPage?XPN=pwVavdhX2CHvfTygFXo9u5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	AU						(ZA200906476)\|NAME=HUNWICK, RICHARD J\|(ZA200906474)\|NAME=HUNWICK, RICHARD J		1	2								(ZA200906476)\|Patent\|(ZA200906474)\|Patent	Titre: (ZA200906476)\|System, apparatus and method for carbon dioxide sequestration Résumé: (ZA200906476)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From CN101641145 A)	13	Abstract	gpt-4o-mini	yes	The process described involves the use of metal silicate rocks to capture CO₂ and produce metal carbonates, which aligns with the topic of enhanced weathering and carbon sequestration.
17	US63/449,791P\|US63/449,791\|WOUS2024/018316	WOUS2024/018316\|JP2025551726\|EP24767679\|KR10-2025-7033809\|AU2024233973\|CA3288102	JP2026510743\|EP4676898\|KR10-2025-0164234\|AU2024233973\|CA3288102\|WO2024/186724	111402698	WO2024/186724 A1 2024-09-12 [WO2024186724]\|JP2026510743 A 2026-04-10 [JP2026510743]\|EP4676898 A1 2026-01-14 [EP4676898]\|KR10-2025-0164234 A 2025-11-24 [KR20250164234]\|AU2024233973 A1 2025-10-23 [AU2024233973]\|CA3288102 A1 2024-09-12 [CA3288102]	2023-03-03\|2024-03-04	2024-03-04\|2024-03-04\|2024-03-04\|2024-03-04\|2024-03-04\|2024-03-04	2026-04-10\|2026-01-14\|2025-11-24\|2025-10-23\|2024-09-12\|2024-09-12		(EP4676898)\|2044-03-04\|(WO2024/186724)\|2026-09-03\|(JP2026510743)\|2044-03-04\|(KR10-2025-0164234)\|2044-03-04\|(AU2024233973)\|2044-03-04\|(CA3288102)\|2044-03-04	(EP4676898)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide	(EP4676898)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.	DARTMOUTH COLLEGE	(EP4676898)\|Trustees of Dartmouth College ([US])\|(WO2024/186724)\|TRUSTEES OF DARTMOUTH COLLEGE ([US])\|(JP2026510743)\|Trustees of Dartmouth College\|(KR10-2025-0164234)\|TRUSTEES OF DARTMOUTH COLLEGE ([US])\|(AU2024233973)\|TRUSTEES OF DARTMOUTH COLLEGE\|(CA3288102)\|TRUSTEES OF DARTMOUTH COLLEGE ([US])	SHARMA MUKUL\|MORRISON BRIAN	(EP4676898)\|SHARMA, Mukul\|MORRISON, Brian	(EP4676898)\|Maiwald GmbH;Engineering ([DE])\|Reg. Nb: 101782373\|(WO2024/186724)\|AMINI, Farhang ([US])\|(JP2026510743)\|YAMAMOTO Osamu\|Reg. Nb: 100118902\|MIYAMAE,Toru\|Reg. Nb: 100106208\|MATSUO JUNICHI\|Reg. Nb: 100196508\|NAKAMURA MITSUTOSHI\|Reg. Nb: 100126985\|(KR10-2025-0164234)\|KIM, JIN HOI\|KIM, TAE HONG\|(AU2024233973)\|PHILLIPS ORMONDE FITZPATRICK ([AU])\|(CA3288102)\|MBM INTELLECTUAL PROPERTY AGENCY ([CA])\|Reg. Nb: e61a1630-b292-4706-b91c-f3098c8c5df7	(WO2024/186724)\|In some embodiments, the methods of the present disclosure also improve the quality of the soil.\|This process is not only beneficial for managing organic matter in the surface and overall grass health, but also will allow basalt sands to penetrate deeper into the surface of the green.\|Ideally, the material should have no particles greater than 1.0 mm in diameter given the difficulty in getting these larger particles to work down into the turf canopy.\|These costs and methods to spread the products for ERW would be especially difficult in places where this spreading is not common practice.\|	(WO2024/186724)\|1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt sand captures the CO2.\|21. A method of modifying a surface, said method comprising: applying a composition comprising at least one basalt sand to the surface, wherein the at least one basalt sand is in the form of crushed particles.\|39. A modified surface, wherein the modified surface comprises a composition, wherein the composition comprises at least one basalt sand, wherein the at least one basalt sand is in the form of crushed particles.\|	(WO2024/186724)\|In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand that is in the form of crushed particles.\|In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand.\|	(WO2024/186724)\|BASALT SAND(100,66)\|SURFACE MODIFICATION(100,36)\|CO2(100,27)\|ENVIRONMENT(100,16)\|CARBON DIOXIDE(100,8)\|TURF MANAGEMENT(100,4)\|ATMOSPHERIC CARBON DIOXIDE(100,1)\|INTEGRATING ENHANCED ROCK(100,1)\|CRUSHED PARTICLE(67,7)\|HOLYOKE BASALT(62,22)\|BASALT(51,69)\|TURF CANOPY(43,1)\|BURNER BASALT(40,13)\|MANAGED TURF(37,10)\|BLUE RIDGE BASALT(32,7)\|GROUND LAYER(25,16)\|ACTINOMYCES(22,5)\|SUBDIVISION(21,6)\|CAAL2SI2O(20,6)\|MICROBE(20,5)\|PYROXENE(19,8)\|HIGHWAY(19,6)\|NAALSI3O(19,6)\|THOLEIITE(18,10)\|GOLF COURSE ADDITIVE(18,7)\|QUARTZ TOP SAND(18,7)\|SPORTS FACILITY(18,6)\|BACTERIA(18,5)\|MANAGING ORGANIC MATTER(18,1)\|PEAT MOSS(17,7)\|SILICATE(17,5)\|ALKALI ION(17,2)\|YARD(16,6)\|PARK(15,6)\|FUNGUS(15,5)\|HEALTH(14,1)\|SURFACE ACRE(13,39)\|LIME(13,8)\|BICARBONATE HCO3(11,2)\|CRUSHED BASALT SAND PARTICLE(11,2)\|PRETREATED BASALT SAND(11,2)\|LARGE PARTICLE(11,1)\|OUTER LAYER(9,25)\|RESIDENTIAL FIELD(9,6)\|CO2 CAPTURE REACTION(9,5)\|CRUSHED BASALT TON(9,1)\|MAFIC APHANITIC VOLCANIC ROCK(9,1)\|PIONEER VALLEY BASALT(9,1)\|ULTRAFINE PARTICLE(8,3)\|USGA ACCREDITED GOLF COURSE(8,3)\|BASALT INTEGRATION(8,2)\|FULL ROOTZONE BASALT(8,2)\|SOIL FERTILIZER(8,2)\|ARTIFICIAL TOPSOIL CREATION(8,1)\|BASALT AMENDED SOIL COLUMN(8,1)\|BASALT SAND DEPLOYMENT(8,1)\|PURCHASED ROCK(7,2)\|MICROSCOPIC PLAGIOCLASE FELDSPAR(7,1)\|GOLF TURF GRASS STUDY(6,1)\|LEVERHULME INSTITUTE(6,1)\|QUICKBIRD IMAGERY(6,1)\|SAND CUSTOM BLEND(6,1)\|SEQUESTRATION OPPORTUNITY(6,1)\|URBAN SUBURBAN LANDSCAPE(6,1)\|USGA RECOMMENDATION(6,1)\|ENHANCED ROCK WEATHERING(5,12)\|FINE GRAINED PARTICLE(5,3)\|CAPTURED CO2(5,2)\|CAPTURING CO2(5,2)\|ENHANCED CO2 CAPTURE(5,2)\|ROCK DUST LOCAL(5,2)\|USGA ROOT ZONE(5,2)\|AGRICULTURAL FARM(5,1)\|AGRICULTURAL SPREADER(5,1)\|ARXIV PREPRINT(5,1)\|BASALT METRIC TON(5,1)\|CACO3 PRECIPITATION(5,1)\|CO2 CONSUMPTION ASSESSMENT(5,1)\|COMMON PRACTICE(5,1)\|EFFLUENT ALKALINITY(5,1)\|EXCHANGEABLE CALCIUM(5,1)\|FINE GRAINED BASALT SAND(5,1)\|MAXIMIZE SEQUESTRATION(5,1)\|MINE TAILING(5,1)\|ROOTZONE SAND(5,1)\|AGRICULTURAL FIELD(4,6)\|HTTP(4,6)\|COURSE GRAINED PARTICLE(4,3)\|MAXIMUM ENHANCED WEATHERING CO2(4,3)\|MEDIUM PARTICLE(4,3)\|MICROPARTICLE(4,3)\|NANOPARTICLE(4,3)\|NUMEROUS LIMITATION(4,3)\|ENHANCED SOIL HEALTH(4,2)\|NONCRYSTALLINE(4,2)\|SOIL FERTILITY ENHANCEMENT(4,2)\|VISIBLE CRYSTAL(4,2)\|AGRICULTURAL ADDITIVE(4,1)\|AGRONOMIC BENEFIT(4,1)\|ANNUAL CAPTURE(4,1)\|APPROVED GREEN ROOTZONE CONSTRUCTION(4,1)\|BASAL SAND(4,1)\|BASALT POWDER RELEASE(4,1)\|CACO3 PRECIPITATE(4,1)\|CAPTURE POTENTIAL ESTIMATE(4,1)\|CIVILIZATION STABILITY(4,1)\|CO2 METRIC TON(4,1)\|CO2 SEQUESTRATION STRATEGY(4,1)\|CO2 SEQUESTRATION TON ACRE(4,1)\|COARSE FRACTION(4,1)\|COARSE PARTICLE(4,1)\|COARSE SAND(4,1)\|CUSTOM BLENDING(4,1)\|DILUTE BASALT(4,1)\|DRAINAGE PIPE(4,1)\|ELUTION EXPERIMENT(4,1)\|EMPIRICAL MONITORING(4,1)\|ESTIMATED CO2 SEQUESTRATION(4,1)\|EXPERIMENT REPORT(4,1)\|EXPERIMENTAL SETUP(4,1)\|FILTERING BASALT(4,1)\|FREQUENT IRRIGATION(4,1)\|GOLF COURSE ANNUAL SAND(4,1)\|MAJOR GEOLOGIC PROVINCE(4,1)\|NATURAL TOPSOIL(4,1)\|REERSHEMIUS PAPER(4,1)\|ROCK POWDER(4,1)\|ROUNDED ESTIMATE(4,1)\|SEA FLOOR(4,1)\|SOIL ADDITIVE(4,1)\|SOIL SAMPLING(4,1)\|SPECIALIZED SPREADING EQUIPMENT(4,1)\|US TON ACRE(4,1)\|VISIBLE PLAGIOCLASE FELDSPAR(4,1)\|WARM CLIMATE(4,1)\|SOIL QUALITY(3,7)\|SUPRA(3,4)\|SOILS(3,3)\|BASALT SAND PARTICLE SIZE(3,2)\|INSULATION(3,2)\|KG CO2(3,2)\|PERIDOTITE(3,2)\|SOIL NUTRIENT(3,2)\|SPRINKLING(3,2)\|AERATION EQUIPMENT(3,1)\|ANGULAR SAND(3,1)\|ATMOSPHERIC CO2 NET REMOVAL(3,1)\|BACKFILL HOLE(3,1)\|BASALT ENHANCED TOP SANDING(3,1)\|BIORAD COLUMN(3,1)\|CO2 SEQUESTRATION POTENTIAL(3,1)\|ENHANCED ROCK WEATHERING RATE(3,1)\|FAIRWAY TOP SANDING(3,1)\|FINE FRACTION(3,1)\|GOLF COURSE SAND SPREADING(3,1)\|HOT CLIMATE(3,1)\|MONITORING SOIL HEALTH(3,1)\|NATIVE ENVIRONMENT(3,1)\|NEGATIVE EMISSION(3,1)\|REDUCING CO2 EMISSION(3,1)\|SOIL UPPER ROOTZONE(3,1)\|STABLE CACO3(3,1)\|FEO(2,3)\|INTEGRATION(2,3)\|ADOPTION(2,1)\|ADSORPTION(2,1)\|AIRSTREAM(2,1)\|ATMOSPHERIC CARBON(2,1)\|BACKFILLING(2,1)\|BASALT WEATHERING(2,1)\|CONSTANT ATTENTION(2,1)\|CONTINENT(2,1)\|COURSE PARTICLE(2,1)\|CROPLAND(2,1)\|DENSE ROOT ZONE(2,1)\|DISTINCTION(2,1)\|ESTABLISHMENT PERIOD(2,1)\|EXPERIMENT TOTAL DURATION(2,1)\|FINE SAND FRACTION(2,1)\|FOUNDATION(2,1)\|FREQUENT TOP BENEFIT(2,1)\|FULL AERATION(2,1)\|\|(JP2026510743)\|BASALT SAND(100,75)\|ACCELERATION(100,3)\|TURF MANAGEMENT(100,3)\|ATMOSPHERIC CARBON DIOXIDE(100,1)\|ROCK INTEGRATION(100,1)\|HOLYOKE BASALT(63,20)\|PULVERIZED BASALT SAND(55,1)\|BURNER BASALT(45,10)\|BLUE RIDGE BASALT(40,6)\|CRUSHED PARTICLE(38,2)\|BASALT(33,58)\|TURF CANOPY(32,1)\|ADDITIVE(31,20)\|ACTINOMYCETE(29,5)\|ERW CDR(28,2)\|MICROORGANISM(27,5)\|PLAGIOCLASE(26,6)\|BIOCHAR(25,5)\|ARTIFICIAL TOPSOIL(25,2)\|PARTICLE PULVERIZATION(24,2)\|BACTERIA(23,5)\|NATURAL TOPSOIL(23,1)\|GROUND(22,30)\|SILICATE(22,5)\|CARBON DIOXIDE CAPTURE(22,2)\|FELDSPAR(21,8)\|PYROXIN(21,8)\|SOLEITE(21,8)\|PEAT MOSS(21,7)\|QUARTZ TOP SAND(21,7)\|FUNGUS(20,5)\|GROUND LAYER(18,16)\|EXCIPIENT(18,3)\|PARTICULATE(18,1)\|LIME(16,8)\|CONCESSION(16,6)\|CAAL2SI2O(15,5)\|CONTROLLED TURF(15,4)\|ENTIRE LAWN(15,1)\|MINERAL NUTRIENT(15,1)\|NUMEROUS LIMITATION(15,1)\|THOLEIITE(15,1)\|NAALSI3O(14,7)\|TOP SAND(13,20)\|GARDEN(13,6)\|HIGHWAY(13,6)\|SPORTS FACILITY(13,6)\|HEALTH(13,1)\|ORGANIC MATTER HEALTH(13,1)\|PHOSPHORUS(13,1)\|GOLF COURSE(12,36)\|ALKALI ION(12,2)\|PERIDOTITE(12,2)\|SURFACE MODIFICATION(11,48)\|PARK(11,6)\|TAILING(11,2)\|NUTRIENT(10,5)\|PIONEER VALLEY BASALT(10,2)\|FARMLAND(10,1)\|SLAG(9,2)\|OUTER LAYER(8,25)\|GRIND BASALT SAND(8,2)\|PRETREATED BASALT SAND(8,2)\|LARGE PARTICLE(8,1)\|AGRICULTURAL LAND(7,5)\|BICARBONATE(7,3)\|ERW(7,3)\|RESIDENTIAL AREA(6,6)\|ROOT ZONE BASALT(6,6)\|CO2 CAPTURE REACTION(6,4)\|COARSE PARTICULATE(6,4)\|MANAGED TURF(6,3)\|USGA CERTIFIED GOLF COURSE(6,3)\|PULVERIZED BASALT(6,2)\|SOIL FERTILIZER(6,2)\|MAFIC AMORPHOUS VOLCANIC ROCK(6,1)\|ROCK WEATHERING PROMOTION INTRODUCTION(6,1)\|BASALT POWDER(5,3)\|ULTRAFINE PARTICULATE(5,2)\|AGRICULTURAL DUSTING(5,1)\|BASALT SAND INTRODUCTION(5,1)\|ERW FEASIBILITY(5,1)\|GROUND BASALT INTRODUCING TON(5,1)\|LAWN NUTRITIONAL BENEFIT(5,1)\|QUICKBIRD IMAGERY(5,1)\|SLOW WEATHERING KINETICS(5,1)\|URBAN SUBURBAN LANDSCAPE(5,1)\|USGA RECOMMENDATION(5,1)\|ORGANIC MATTER(4,5)\|COARSE PARTICLE(4,2)\|ROCK DUST LOCAL(4,2)\|ARXIV PREPRINT(4,1)\|ERW STRATEGY(4,1)\|EXCHANGEABLE CALCIUM(4,1)\|FINE GRAINED BASALT SAND(4,1)\|USGA RECOMMENDED ROOT REGION(4,1)\|INCORPORATION(3,8)\|BASALT ENHANCED TOP SANDING(3,3)\|GOLF COURSE CERTIFICATION(3,3)\|NANOPARTICLE(3,3)\|ENHANCED SOIL HEALTH(3,2)\|MICROPARTICULATE(3,2)\|ROCK POWDER(3,2)\|SOIL FERTILITY ENHANCEMENT(3,2)\|SOIL PH OPTIMIZATION(3,2)\|AGRICULTURAL ADDITIVE(3,1)\|AGRONOMIC BENEFIT(3,1)\|ANNUAL COURSE SANDING(3,1)\|ARTIFICIAL TOPSOIL FORMATION(3,1)\|BASALT CONSUMPTION(3,1)\|BASALT INTRODUCTION(3,1)\|CAPTURE POTENTIAL ESTIMATE(3,1)\|CITED DOCUMENT(3,1)\|CIVILIZATION STABILITY(3,1)\|COARSE FRACTION(3,1)\|DILUTE BASALT(3,1)\|DISASTER CLASS IMPACT(3,1)\|EMPIRICAL MONITORING(3,1)\|FILTERING BASALT(3,1)\|FREQUENT IRRIGATION(3,1)\|FUNDAMENTAL THREAT(3,1)\|GOLF TURF(3,1)\|HEALTH MONITORING(3,1)\|ISOLATION STRATEGY(3,1)\|LABORATORY EXPERIMENT(3,1)\|MAXIMIZE ISOLATION(3,1)\|PREEXISTING SUB SOIL(3,1)\|REPORTER ASSAY(3,1)\|ROCK INCORPORATION(3,1)\|ROUGH SAND(3,1)\|ROUGHNESS PARTICLE(3,1)\|ROUNDED ESTIMATE(3,1)\|SEA FLOOR(3,1)\|SOIL ADDITIVE(3,1)\|SOIL SAMPLING(3,1)\|SOILS PH(3,1)\|TON INTRODUCTION(3,1)\|TURF ROOT REGION(3,1)\|US TON ACRE(3,1)\|SOIL QUALITY(2,7)\|SURFACE SOIL(2,6)\|HTTP(2,5)\|AERATION(2,3)\|GRINDING(2,3)\|GROUND SURFACE(2,3)\|NAKED EYE(2,3)\|AL2SI2O(2,2)\|GOLF COURSE ADDITIVE(2,2)\|MEDIUM PARTICULATE(2,2)\|METRIC TON(2,2)\|SCIENTIFIC LITERATURE(2,2)\|SOIL NUTRIENT(2,2)\|SPRINKLING(2,2)\|ULTRAFINE PARTICLE(2,2)\|ANGULAR SAND(2,1)\|BASALT MODIFIED SOIL(2,1)\|DISCLOSURE CAPTURE(2,1)\|ENHANCED ROCK WEATHERING RATE(2,1)\|ERWS COST(2,1)\|FAIRWAY TOP SANDING(2,1)\|FINE FRACTION(2,1)\|GOLF COURSE SAND SPRAYING(2,1)\|HOT CLIMATE(2,1)\|MAINTAINING PRODUCTIVITY(2,1)\|NET ATMOSPHERE(2,1)\|PERIODIC CARE(2,1)\|PLAGIOCLASE FELDSPAR(2,1)\|SIMULATION(2,1)\|STABLE CACO(2,1)\|TOP SANDING ADOPTION(2,1)\|2H4SIO(1,1)\|ACCESSORY(1,1)\|ADSORPTION(1,1)\|ALKALINITY(1,1)\|ASSESSMENT(1,1)\|ATMOSPHERIC CARBON(1,1)\|BASALT CHEMICAL COMPOSITION(1,1)\|BASALT CURRENT(1,1)\|BASALT SAND PARTICLE SIZE(1,1)\|CLIMATE CHANGE IMPACT(1,1)\|\|(KR10-2025-0164234)\|BASALT SAND(100,54)\|CARBON DIOXIDE(100,8)\|LAWN MANAGEMENT(100,3)\|STRENGTHENING INTEGRATION(100,1)\|CRUSHED PARTICLE(72,7)\|BASALT SAND CAPTURE(67,1)\|HOLYOAK BASALT(61,19)\|BASALT(46,80)\|LAWN CANOPY(41,1)\|BERTNER BASALT(35,8)\|BLUE RIDGE BASALT(32,7)\|GRASS(28,32)\|GROUND LAYER(25,16)\|BURNER BASALT(24,2)\|ACTINOMYCETE(23,5)\|MICROORGANISM(23,4)\|SPARGING PRODUCT(22,1)\|SPARGING(21,1)\|PARCEL(20,3)\|NAALSI3O(19,6)\|LITHOGRAPH(19,2)\|FARMLAND(18,7)\|GOLF COURSE ADDITIVE(18,7)\|SPORTS FACILITY(18,6)\|BACTERIA(18,5)\|PEAT MOSS(18,5)\|QUARTZ TOP SAND(17,7)\|ALKALI ION(17,2)\|HIGHWAY(16,6)\|SILICATE(16,5)\|SURFACE MODIFICATION(15,38)\|FUNGUS(15,5)\|PLAGIOCLASE FELDSPAR(15,2)\|ERWS(15,1)\|PARK(14,6)\|YARD(14,6)\|SOLEITE(14,5)\|LIME(13,7)\|PRETREATED BASALT SAND(11,2)\|PYROXENE(11,2)\|LARGE PARTICLE(11,1)\|OUTER LAYER(10,23)\|COARSE PARTICLE(10,7)\|ACRE TON SURFACE(10,2)\|CRUSHED BASALT INJECTING TON(10,1)\|BICARBONATE(9,3)\|BUTTNER BASALT(9,3)\|HAYLOOK BASALT(9,2)\|ATMOSPHERIC CO2(9,1)\|HOLYOAK BASALT RIDGE(9,1)\|MAFIC APLASTIC VOLCANIC ROCK(9,1)\|PIONEER VALLEY BASALT(9,1)\|MANAGED TURF(8,3)\|USGA CERTIFIED GOLF COURSE(8,3)\|ARTIFICIAL TOPSOIL CREATION(8,1)\|COMMINUTED BASALT SAND PARTICLE(8,1)\|INTEGRATING BASALT SAND(8,1)\|ANNUAL SURFACE ACRE(7,21)\|RESIDENTIAL AREA(7,6)\|BASALT POWDER(7,3)\|GRIND BASALT SAND(7,1)\|STRENGTHENING ROCK INTEGRATION(7,1)\|SURFACE TON ACRE(7,1)\|PETE MOSS(6,2)\|PURCHASED ROCK(6,2)\|ERW CDR(6,1)\|ERW FEASIBILITY(6,1)\|MAJOR GEOLOGICAL GEOGRAPHY(6,1)\|QUICKBIRD IMAGERY(6,1)\|SAND CUSTOM BLEND(6,1)\|SLOW WEATHERING KINETICS(6,1)\|TOPSOIL ROOTZONE(6,1)\|URBAN SUBURBAN LANDSCAPE(6,1)\|USGA RECOMMENDATION(6,1)\|CAPTURE REACTION(5,5)\|GOLF COURSE CERTIFICATION(5,4)\|ULTRAFINE PARTICLE(5,3)\|LIMITATION CAAL2SI2O(5,2)\|ROCK DUST LOCAL(5,2)\|ROCK POWDER(5,2)\|AGRICULTURAL SPRAYER(5,1)\|ARXIV PREPRINT(5,1)\|BASALT METRIC TON(5,1)\|CACO PRECIPITATION(5,1)\|EFFLUENT ALKALINITY(5,1)\|ERW STRATEGY(5,1)\|EXCHANGEABLE CALCIUM(5,1)\|FINE BASALT SAND(5,1)\|FULL ROOTZONE BASALT(5,1)\|GROUND BASALT SAND PARTICLE(5,1)\|HOLIOKE BASALT(5,1)\|MANAGED GRASS(5,1)\|MAXIMIZE SEQUESTRATION(5,1)\|PORE BACKFILLING(5,1)\|SAND USAGE ESTIMATE(5,1)\|SOIL FERTILIZER(5,1)\|HTTP(4,6)\|MEDIUM PARTICLE(4,3)\|MICROPARTICLE(4,3)\|NANOPARTICLE(4,3)\|VISIBLE CRYSTAL(4,2)\|AGRICULTURAL ADDITIVE(4,1)\|AGRONOMIC BENEFIT(4,1)\|CAPTURE CO2(4,1)\|CIVILIZATION STABILITY(4,1)\|COARSE GRAINED PARTICLE(4,1)\|COARSE SAND(4,1)\|CUSTOM BLENDING(4,1)\|DILUTE BASALT(4,1)\|ELUTION EXPERIMENT(4,1)\|EMPIRICAL MONITORING(4,1)\|FACILITY INFRASTRUCTURE(4,1)\|FILTERING BASALT(4,1)\|FINE SANDSTONE(4,1)\|FREQUENT IRRIGATION(4,1)\|GOLF LAWN GRASS(4,1)\|GOLF TURF(4,1)\|GRASS MANAGEMENT(4,1)\|GRAY STONE(4,1)\|ISOLATION STRATEGY(4,1)\|LABORATORY EXPERIMENT(4,1)\|MANAGED LAWN(4,1)\|NATURAL TOPSOIL(4,1)\|REERSHEMIUS PAPER(4,1)\|ROUNDED ESTIMATE(4,1)\|SOIL ADDITIVE(4,1)\|SOIL SAMPLING(4,1)\|SPECIALIZED SPRAY EQUIPMENT(4,1)\|TON INJECTION(4,1)\|US TON ACRE(4,1)\|VISIBLE SANDSTONE(4,1)\|SPRAYING(3,5)\|BASALT SAND PARTICLE SIZE(3,2)\|GUIDANCE(3,2)\|NORTH(3,2)\|PERIDOTITE(3,2)\|AERATION EQUIPMENT(3,1)\|ANGLED SAND(3,1)\|ANNUAL FULL COURSE SANDING(3,1)\|BASALT ENHANCED TOP SANDING(3,1)\|BIORAD COLUMN(3,1)\|ENHANCED ROCK WEATHERING RATE(3,1)\|ENTIRE PLANTING LAYER BASALT(3,1)\|EXPERIMENT TOTAL DURATION(3,1)\|FAIRWAY TOP SANDING(3,1)\|FINE GRAINED PARTICLE(3,1)\|GUIDELINE(3,1)\|HOT CLIMATE(3,1)\|MAXIMUM REINFORCEMENT(3,1)\|MONITORING SOIL HEALTH(3,1)\|NEGATIVE EMISSION(3,1)\|PLANT BED(3,1)\|SIMULATION(3,1)\|SOIL COLUMN(3,1)\|SPREADING EQUIPMENT(3,1)\|STABLE CACO(3,1)\|ULTRAFINE RATIO(3,1)\|UNIFORM MODULUS(3,1)\|FEO(2,3)\|GRINDING(2,3)\|INTEGRATION(2,3)\|ADSORPTION(2,1)\|ASSESSMENT(2,1)\|BASALT WEATHERING(2,1)\|CO2 REMOVAL(2,1)\|COARSE RATIO(2,1)\|COMBINING REACTION(2,1)\|COMMINUTING(2,1)\|COMMINUTION(2,1)\|CONTINENT(2,1)\|DISTINCTION(2,1)\|DRAINPIPE(2,1)\|\|(AU2024233973)\|BASALT SAND(100,58)\|HOLYOKE BASALT(61,21)\|CRUSHED PARTICLE(54,5)\|BASALT(45,60)\|TURF CANOPY(42,1)\|BURNER BASALT(39,12)\|MANAGED TURF(36,10)\|BLUE RIDGE BASALT(33,6)\|GROUND LAYER(25,16)\|SUBDIVISION(21,6)\|ACTINOMYCES(21,5)\|PYROXENE(19,7)\|HIGHWAY(19,6)\|CAAL2SI(19,5)\|MICROBE(19,5)\|CO2(18,18)\|THOLEIITE(18,9)\|GOLF COURSE ADDITIVE(18,7)\|QUARTZ TOP SAND(18,7)\|SPORTS FACILITY(18,6)\|BACTERIA(18,5)\|NAALSI(18,5)\|PEAT MOSS(17,7)\|ALKALI ION(17,2)\|MANAGING ORGANIC MATTER(17,1)\|YARD(16,6)\|SILICATE(16,5)\|SURFACE MODIFICATION(15,34)\|PARK(15,6)\|FUNGUS(15,5)\|SURFACE ACRE(13,39)\|LIME(13,8)\|HEALTH(13,1)\|REGULAR TOPSANDING AERATION(11,2)\|LARGE PARTICLE(11,1)\|OUTER LAYER(9,23)\|RESIDENTIAL FIELD(9,6)\|BICARBONATE(9,3)\|MAFIC APHANITIC VOLCANIC ROCK(9,1)\|PIONEER VALLEY BASALT(9,1)\|CO2 CAPTURE REACTION(8,4)\|USGA ACCREDITED GOLF COURSE(8,3)\|BASALT INTEGRATION(8,2)\|FULL ROOTZONE BASALT(8,2)\|SOIL FERTILIZER(8,2)\|ARTIFICIAL TOPSOIL CREATION(8,1)\|BASALT AMENDED SOIL COLUMN(8,1)\|BASALT SAND DEPLOYMENT(8,1)\|CRUSHED BASALT SAND PARTICLE(8,1)\|CRUSHED BASALT TON(8,1)\|PRETREATED BASALT SAND(8,1)\|CARBON DIOXIDE(7,4)\|COARSE GRAVEL FINE GRAVEL(7,1)\|COARSE SAND COARSE SAND(7,1)\|MICROSCOPIC PLAGIOCLASE FELDSPAR(7,1)\|PURCHASED ROCK(6,2)\|ULTRAFINE PARTICLE(6,2)\|GOLF TURF GRASS STUDY(6,1)\|LEVERHULME INSTITUTE(6,1)\|QUICKBIRD IMAGERY(6,1)\|SAND CUSTOM BLEND(6,1)\|SEQUESTRATION OPPORTUNITY(6,1)\|URBAN SUBURBAN LANDSCAPE(6,1)\|USGA RECOMMENDATION(6,1)\|ENHANCED ROCK WEATHERING(5,12)\|CAPTURED CO2(5,2)\|CAPTURING CO2(5,2)\|ENHANCED CO2 CAPTURE(5,2)\|ROCK DUST LOCAL(5,2)\|USGA ROOT ZONE(5,2)\|AGRICULTURAL FARM(5,1)\|AGRICULTURAL SPREADER(5,1)\|ARXIV PREPRINT(5,1)\|BACKFILL AERATION(5,1)\|BASALT METRIC TON(5,1)\|BASALT TON YEAR(5,1)\|CACO3 PRECIPITATION(5,1)\|CLAY ROOTZONE(5,1)\|CO2 CONSUMPTION ASSESSMENT(5,1)\|COMMON PRACTICE(5,1)\|EFFLUENT ALKALINITY(5,1)\|EXCHANGEABLE CALCIUM(5,1)\|FINE GRAINED BASALT SAND(5,1)\|MAXIMIZE SEQUESTRATION(5,1)\|MINE TAILING(5,1)\|ROOTZONE SAND(5,1)\|SQ FT YEAR EAR(5,1)\|TBASALT CO2 SEQUESTRATION POTENTIAL(5,1)\|UNIFORMITY CLAY COEFFICIENT(5,1)\|AGRICULTURAL FIELD(4,6)\|HTTP(4,6)\|MAXIMUM ENHANCED WEATHERING CO2(4,3)\|TURF MANAGEMENT(4,3)\|ENHANCED SOIL HEALTH(4,2)\|FINE GRAINED PARTICLE(4,2)\|NONCRYSTALLINE(4,2)\|SOIL FERTILITY ENHANCEMENT(4,2)\|VISIBLE CRYSTAL(4,2)\|AGRICULTURAL ADDITIVE(4,1)\|AGRONOMIC BENEFIT(4,1)\|ALKALINITY CO2(4,1)\|ANNUAL CAPTURE(4,1)\|APPROVED GREEN ROOTZONE CONSTRUCTION(4,1)\|BASAL SAND(4,1)\|BASALT POWDER RELEASE(4,1)\|BASALT YEAR METRIC TON(4,1)\|CACO3 PRECIPITATE(4,1)\|CAPTURE POTENTIAL ESTIMATE(4,1)\|CIVILIZATION STABILITY(4,1)\|CO2 METRIC TON(4,1)\|CO2 SEQUESTRATION METRIC TON(4,1)\|CO2 SEQUESTRATION STRATEGY(4,1)\|COARSE FRACTION(4,1)\|COARSE PARTICLE(4,1)\|CUSTOM BLENDING(4,1)\|DILUTE BASALT(4,1)\|DRAINAGE PIPE(4,1)\|ELUTION EXPERIMENT(4,1)\|EMPIRICAL MONITORING(4,1)\|ESTIMATED CO2 SEQUESTRATION(4,1)\|EXPERIMENT REPORT(4,1)\|EXPERIMENTAL SETUP(4,1)\|FILTERING BASALT(4,1)\|FREQUENT IRRIGATION(4,1)\|GOLF COURSE ANNUAL SAND(4,1)\|MAJOR GEOLOGIC PROVINCE(4,1)\|NATURAL TOPSOIL(4,1)\|PLANAV SKY(4,1)\|REERSHEMIUS PAPER(4,1)\|ROCK POWDER(4,1)\|ROOTZONE W INORGANIC AMENDMENT(4,1)\|ROUNDED ESTIMATE(4,1)\|SEA FLOOR(4,1)\|SOIL SAMPLING(4,1)\|SPECIALIZED SPREADING EQUIPMENT(4,1)\|US TON ACRE(4,1)\|VISIBLE PLAGIOCLASE FELDSPAR(4,1)\|WARM CLIMATE(4,1)\|SOIL QUALITY(3,7)\|SUPRA(3,4)\|SOILS(3,3)\|BASALT SAND PARTICLE SIZE(3,2)\|COURSE GRAINED PARTICLE(3,2)\|INSULATION(3,2)\|KG CO2(3,2)\|MEDIUM PARTICLE(3,2)\|MICROPARTICLE(3,2)\|NANOPARTICLE(3,2)\|NUMEROUS LIMITATION(3,2)\|PERIDOTITE(3,2)\|SOIL NUTRIENT(3,2)\|SPRINKLING(3,2)\|AERATION EQUIPMENT(3,1)\|ANGULAR SAND(3,1)\|ATMOSPHERIC CO2 NET REMOVAL(3,1)\|BACKFILL HOLE(3,1)\|BASALT ENHANCED TOP SANDING(3,1)\|BIORAD COLUMN(3,1)\|ENHANCED ROCK WEATHERING RATE(3,1)\|FAIRWAY TOP SANDING(3,1)\|FINE FRACTION(3,1)\|FINE SAND SILT(3,1)\|GOLF COURSE SAND SPREADING(3,1)\|HOT CLIMATE(3,1)\|MONITORING SOIL HEALTH(3,1)\|NATIVE ENVIRONMENT(3,1)\|NEGATIVE EMISSION(3,1)\|REDUCING CO2 EMISSION(3,1)\|SOIL UPPER ROOTZONE(3,1)\|STABLE CACO3(3,1)\|W PEAT SIEVE(3,1)\|INTEGRATION(2,3)\|ADOPTION(2,1)\|ADSORPTION(2,1)\|AIRSTREAM(2,1)\|ATMOSPHERIC CARBON(2,1)\|BACKFILLING(2,1)\|BASALT WEATHERING(2,1)\|CARBON OFFSET PRICE(2,1)\|COMBINING REACTION(2,1)\|CONSTANT ATTENTION(2,1)\|CONTINENT(2,1)\|COURSE PARTICLE(2,1)\|CROPLAND(2,1)\|DENSE ROOT ZONE(2,1)\|DISTINCTION(2,1)\|ESTABLISHMENT PERIOD(2,1)\|EXPERIMENT TOTAL DURATION(2,1)\|FINE SAND FRACTION(2,1)\|FOUNDATION(2,1)\|FREQUENT TOP BENEFIT(2,1)\|FULL AERATION(2,1)\|	(WO2024/186724)\|CLAIMS \|1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt sand captures the CO2.\|2. The method of claim 1, wherein the at least one basalt sand is in purified form.\|3. The method of claim 1, wherein the at least one basalt sand comprises a plurality of different types of basalt sands.\|4. The method of claim 1, wherein the at least one basalt sand is selected from the group consisting of plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalt, or combinations thereof.\|5. The method of claim 1, wherein the at least one basalt sand comprises Holyoke Basalt.\|6. The method of claim 1, wherein the at least one basalt sand comprises a compound selected from the group consisting of CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof.\|7. The method of claim 1, wherein the composition further comprises one or more additives.\|8. The method of claim 7, wherein the one or more additives is selected from the group consisting of silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof.\|9. The method of claim 1, wherein the exposing occurs by applying the composition to a surface.\|10. The method of claim 9, wherein the method further comprises removing an outer layer of the surface prior to applying the composition to the surface.\|11. The method of claim 9, wherein the composition is placed on an outer layer of the surface.\|12. The method of claim 9, wherein the composition is applied at a concentration of at least about 25 ton per acre of the surface per year.\|13. The method of claim 9, wherein the surface comprises soil.\|14. The method of claim 13, wherein the soil is selected from the group consisting of top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof.\|15. The method of claim 13, wherein the soil comprises a soil layer below grass.\|16. The method of claim 9, wherein the surface comprises a field.\|17. The method of claim 16, wherein the field comprises an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof.\|18. The method of claim 16, wherein the field comprises a golf course.\|19. The method of claim 1, wherein the CO2 comprises atmospheric CO2.\|20. The method of claim 1, wherein the CO2 capture occurs by a reaction between the at least one basalt sand, CO2, and water, wherein the reaction releases one or more alkaline ions and mineralized bicarbonate (HCO3-).\|21. A method of modifying a surface, said method comprising: applying a composition comprising at least one basalt sand to the surface, wherein the at least one basalt sand is in the form of crushed particles.\|22. The method of claim 21, wherein the at least one basalt sand is in purified form.\|23. The method of claim 21, wherein the at least one basalt sand comprises a plurality of different types of basalt sands.\|24. The method of claim 21, wherein the at least one basalt sand is selected from the group consisting of plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalt, or combinations thereof.\|25. The method of claim 21, wherein the at least one basalt sand comprises Holyoke Basalt.\|26. The method of claim 21, wherein the at least one basalt sand comprises a compound selected from the group consisting of CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof.\|27. The method of claim 21, wherein the composition further comprises one or more additives.\|28. The method of claim 27, wherein the one or more additives is selected from the group consisting of silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof.\|29. The method of claim 21, wherein the exposing occurs by applying the composition to a surface.\|30. The method of claim 29, wherein the method further comprises removing an outer layer of the surface prior to applying the composition to the surface.\|31. The method of claim 29, wherein the composition is placed on an outer layer of the surface.\|32. The method of claim 29, wherein the composition is applied at a concentration of at least about 25 tons per acre of the surface per year.\|33. The method of claim 29, wherein the surface comprises soil.\|34. The method of claim 33, wherein the soil is selected from the group consisting of top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof.\|35. The method of claim 33, wherein the soil comprises a soil layer below grass.\|36. The method of claim 29, wherein the surface comprises a field.\|37. The method of claim 36, wherein the field comprises an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof.\|38. The method of claim 36, wherein the field comprises a golf course.\|39. A modified surface, wherein the modified surface comprises a composition, wherein the composition comprises at least one basalt sand, wherein the at least one basalt sand is in the form of crushed particles.\|40. The modified surface of claim 39, wherein the at least one basalt sand is in purified form.\|41. The modified surface of claim 39, wherein the at least one basalt sand comprises a plurality of different types of basalt sands.\|42. The modified surface of claim 39, wherein the at least one basalt sand is selected from the group consisting of plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalt, or combinations thereof.\|43. The modified surface of claim 39, wherein the at least one basalt sand comprises Holyoke Basalt.\|44. The modified surface of claim 39, wherein the at least one basalt sand comprises a compound selected from the group consisting of CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof.\|45. The modified surface of claim 39, wherein the composition further comprises one or more additives.\|46. The modified surface of claim 45, wherein the one or more additives is selected from the group consisting of silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof.\|47. The modified surface of claim 39, wherein the composition is positioned on an outer layer of the surface.\|48. The modified surface of claim 39, wherein the composition is at a concentration of at least about 25 tons per acre of the surface.\|49. The modified surface of claim 39, wherein the surface comprises soil.\|50. The modified surface of claim 49, wherein the soil is selected from the group consisting of top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof.\|51. The modified surface of claim 49, wherein the soil comprises a soil layer below grass.\|52. The modified surface of claim 39, wherein the surface is associated with a field.\|53. The modified surface of claim 52, wherein the field comprises an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof.\|54. The modified surface of claim 52, wherein the field comprises a golf course.	(WO2024/186724)\| INTEGRATING ENHANCED ROCK WEATHERING AND TURF MANAGEMENT TO SEQUESTER ATMOSPHERIC CARBON DIOXIDE CROSS-REFERENCE TO RELATED APPLICATIONS \|[0001] The present application claims the benefit of U.S. Provisional Patent Application No. 63/449,791, filed on March 3, 2023. The entirety of the aforementioned application is incorporated herein by reference. BACKGROUND \|[0002] Current methods of capturing carbon dioxide (CO2) have numerous limitations in terms of efficacy, efficiency, costs, and the ability to capture CO2 at a large scale. Numerous embodiments of the present disclosure address the aforementioned limitations. SUMMARY \|[0003] In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand that is in the form of crushed particles. In some embodiments, the basalt sand is in purified form. In some embodiments, the basalt sand includes pre-treated basalt sand. In some embodiments, the basalt sand includes a plurality of different types of basalt sands. In some embodiments, the basalt sands of the present disclosure may be in the form of course particles, medium particles, course- grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. In some embodiments, the basalt sands may be mixed with other sands and/or soil additives. \|[0004] The basalt sands of the present disclosure may include various compounds. For instance, in some embodiments, the compounds may include, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof. In some embodiments, the basalt sand compositions of the present disclosure include, without limitation, plagioclase feldspars-containing basalt, pyroxenes-containing basalt, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof.\|[0005] Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. In some embodiments, the compositions of the present disclosure are placed on an outer layer of the surface. In some embodiments, the methods of the present disclosure may also include a step of removing an outer layer of a surface prior to applying a composition of the present disclosure to the surface. In some embodiments, the methods of the present disclosure also include a step of integrating the compositions of the present disclosure with a surface (e.g., within the topsoil and/or rootzone of a turf). \|[0006] Additional embodiments of the present disclosure pertain to modified surfaces that include a composition of the present disclosure. Further embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure. \|[0007] Additional embodiments of the present disclosure pertain to methods of making the basalt sand compositions of the present disclosure. In some embodiments, such methods include crushing at least one basalt sand such that the crushing results in the formation of crushed basalt sand particles. In some embodiments, the methods of the present disclosure also include a step of isolating, filtering, and/or drying the basalt sand. DESCRIPTION OF THE DRAWINGS \|[0008] FIGS. 1A-1C illustrate an exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a full rootzone basalt sand integration process. \|[0009] FIGS.2A-2B illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a top sand only basalt sand integration process. \|[0010] FIGS.3A-3C illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a basalt enhanced top sanding and aeration process, which can be used as part of ongoing aeration and top sanding programs to form a modified surface. \|[0011] FIGS.4A-4C illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a full rootzone basalt sand integration process.\|[0012] FIG.5 illustrates the locations of top 99 Golf Courses in the United States in relation to three major geologic provinces with basalt. \|[0013] FIG. 6 shows the particle size distribution of Pioneer Valley basalt from Rock Dust Local (rockustlocal.com). \|[0014] FIGS.7A-7B provide an experimental setup (FIG. 7A) and experimental results (FIG.7B) demonstrating that soil amended with basalt powder releases six-times more alkalinity than the control soil. DETAILED DESCRIPTION \|[0015] It is to be understood that both the foregoing general description and the following detailed description are illustrative and explanatory, and are not restrictive of the subject matter, as claimed. In this application, the use of the singular includes the plural, the word “a” or “an” means “at least one”, and the use of “or” means “and/or”, unless specifically stated otherwise. Furthermore, the use of the term “including”, as well as other forms, such as “includes” and “included”, is not limiting. Also, terms such as “element” or “component” encompass both elements or components comprising one unit and elements or components that include more than one unit unless specifically stated otherwise. \|[0016] The section headings used herein are for organizational purposes and are not to be construed as limiting the subject matter described. All documents, or portions of documents, cited in this application, including, but not limited to, patents, patent applications, articles, books, and treatises, are hereby expressly incorporated herein by reference in their entirety for any purpose. In the event that one or more of the incorporated literature and similar materials defines a term in a manner that contradicts the definition of that term in this application, this application controls. \|[0017] Climate change fundamentally threatens the safety and stability of modern civilization. In order to avoid the increasingly disastrous and costly effects of climate change, net atmospheric concentrations of greenhouse gases must be reduced. Such reductions can be achieved through improvements in productive efficiency (e.g., reducing CO2 emissions while maintaining output) and carbon dioxide (CO2) removal (CDR).\|[0018] Enhanced rock weathering (ERW) is an example of a CDR-based approach that aims to take atmospheric Carbon (CO2) out of air and store it as bicarbonate or carbonate. ERW has been investigated in cropland but not in golf courses or other managed turfs. Several different types of materials have been used for ERW, including peridotite, basalt, slag, and mine-tailings. Furthermore, ERW has beneficial effects on soil health by releasing beneficial mineral nutrients into the soil, such as calcium, potassium, phosphorous, and magnesium. \|[0019] However, ERW-based CDR processes utilizing peridotites, mine tailings, slag, and basalt other than tholeiites have numerous limitations. Foremost among them is the potential release of heavy metals to the environment and slow weathering kinetics. Furthermore, manufacturing large amounts of basalt powder (including mining, crushing, sorting, and shipping) can be an energy intensive process. Moreover, there is additional energy required to apply the basalt powder multiple times throughout the growing season with specialized spreading equipment that is typically gas powered. These costs and methods to spread the products for ERW would be especially difficult in places where this spreading is not common practice. This results in increased development costs and increased energy consumption. Such limitations may render ERW-based CDR processes inefficient and impractical for large scale CO2 capture from large surface areas. \|[0020] In comparison, golf course greens and courses at large, which, in general, are intensively managed, already engage in this top sanding process. They own and have the technical expertise to spread large amounts of sand onto the turf surface and rootzone. There are large amounts of research into turf grass and golf course maintenance practices aiding the development and deployment of basalt sands within existing maintenance and construction. Additionally, Golf courses have many characteristics that make them ideal to engender CDR through ERW as they are frequently located in warm and hot climates, are frequently watered and receive precipitation, and have high levels of primary productivity leading to turfs generating large amounts of organic matter—three parameters that increase the weathering rate. \|[0021] In sum, current methods of capturing CO2 have numerous limitations in terms of efficacy, efficiency, costs, and the ability to capture CO2 from large surface areas. Numerous embodiments of the present disclosure address the aforementioned limitations. \|[0022] Basalt sand compositions\|[0023] In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand. Basalt is the name of a mafic aphanitic volcanic rock that includes, without limitation, tholeiites. Basalt is exposed around the world on the continents and at the ocean floor. The basalt sands of the present disclosure may be in various forms. For instance, in some embodiments, the basalt sand is in isolated form (i.e., basalt sand isolated from its native environment). In some embodiments, the basalt sand is in the form of crushed particles. In some embodiments, the basalt sand is in purified form. In some embodiments, the basalt sand includes pre-treated basalt sand. In some embodiments, the basalt sands of the present disclosure may be in the form of course particles, medium particles, course-grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. \|[0024] The basalt sands of the present disclosure may include various compounds. For instance, in some embodiments, the compounds may include, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof. \|[0025] The compositions of the present disclosure may include various types of basalt sands. In some embodiments the basalt sand includes a plurality of different types of basalt sands. In some embodiments, the basalt sand includes, without limitation, plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. \|[0026] In some embodiments, the basalt sand compositions of the present disclosure include plagioclase feldspars-containing basalts and pyroxenes-containing basalts. In some embodiments, the basalt sand compositions of the present disclosure include microscopic or visible plagioclase feldspars-containing basalts and pyroxenes-containing basalts, with little or no olivines, and with minor iron spinel and phosphate. \|[0027] In some embodiments, the basalt sand compositions of the present disclosure include tholeiites. In some embodiments, the basalt sand compositions of the present disclosure include tholeiites with low heavy metal concentrations.\|[0028] In some embodiments, the basalt sand compositions of the present disclosure include Holyoke Basalt. In some embodiments, the Holyoke Basalt is derived from Massachusetts (MA). In some embodiments, the average concentrations of Cr, Ni, Cu, Zn, and Pb in Holyoke Basalt are 13 ppm, 33 ppm, 78 ppm, 86 ppm, and 4 ppm, respectively. In some embodiments, the average concentrations of Cr, Ni, Cu, Zn, and Pb in Holyoke Basalt are 384 ppm, 75 ppm, 145 ppm, 88 ppm, and 1.5 ppm, respectively. In some embodiments, Holyoke Basalt is essentially devoid of visible crystals. In some embodiments, Holyoke Basalt is in non-crystalline form. In some embodiments, Holyoke Basalt includes the following elements: SiO2, TiO2, Al2O3, Fe2O3, FeO, CaO, MgO, MnO, K2O, Na2O, and P2O5. \|[0029] In some embodiments, the basalt sand compositions of the present disclosure include Butner Basalt. In some embodiments, the Butner Basalt is derived from North Carolina (NC). In some embodiments, Butner Basalt is essentially devoid of visible crystals. In some embodiments, Butner Basalt is in non-crystalline form. \|[0030] In some embodiments, Holyoke Basalt and Butner Basalt each include the following elements: SiO2, TiO2, Al2O3, Fe2O3, FeO, CaO, MgO, MnO, K2O, Na2O, and P2O5. In some embodiments, the aforementioned elements are present at average weight percentages listed in Table 1. Table 1. Average weight percentages of major elements of Holyoke and Butner Basalts. The data are averages of published results downloaded from GEOROC.org. () FeO for Butner basalt reflects the total amount of iron present without making a distinction between Fe(II) and Fe(III). (*) EPOT is the maximum enhanced weathering CO2 capture potential in units of kg CO2 t-1 (as defined in Renforth (2019) The negative emission potential of alkaline materials. Nature Comm. https://doi.org/10.1038/s41467-019-09475-5). \|[0031] The basalt sands of the present disclosure may include various particle shapes. For instance, in some embodiments, the basalt sand particles of the present disclosure may be angular or rounded depending on their application. In some embodiments, different proportions of basalt sand particle sizes and blends may be used to best suit the local conditions. For instance, in some embodiments, finer sands may retain more moisture within an upper rootzone of a soil. In some embodiments, such sands may also include reduced moisture content through various treatment methods (e.g., kiln drying) so that they can be applied to a surface more effectively (e.g., more efficient spreading using golf course sand spreading and aeration equipment). \|[0032] The compositions of the present disclosure may also include additional components. For instance, in some embodiments, the compositions of the present disclosure may also include one or more additives. In some embodiments, the one or more additives include, without limitation, silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz- based top sands, lime, or combinations thereof.\|[0033] In some embodiments, the additives include one or more golf course additives. In some embodiments, the golf course additives include, without limitation, peat moss, quartz-based top sands, lime, or combinations thereof. In some embodiments, the quartz-based top sands are utilized to dilute the basalt. In some embodiments, the basalt sand compositions of the present disclosure may be treated with such additives depending on the needs of a surface (e.g., a local soil). \|[0034] Methods of modifying a surface \|[0035] Additional embodiments of the present disclosure pertain to methods of modifying a surface. In some embodiments, such methods include applying a composition of the present disclosure to the surface. Suitable compositions were described supra and are incorporated herein by reference. \|[0036] The compositions of the present disclosure may be applied to surfaces in various manners. For instance, in some embodiments, the compositions of the present disclosure may be applied by methods that include, without limitation, spreading, pouring, sprinkling, spraying, or combinations thereof. In some embodiments, the compositions of the present disclosure are placed on an outer layer of the surface. In some embodiments, the compositions of the present disclosure may become integrated with the surface. In some embodiments, the methods of the present disclosure may also include a step of removing an outer layer of a surface prior to applying a composition of the present disclosure to the surface. \|[0037] FIGS. 1A-1C, 2A-2B, 3A-3C, and 4A-4C illustrate exemplary processes for applying a composition of the present disclosure to a surface. For instance, FIGS.1A-1C illustrate an exemplary process for applying a composition of the present disclosure (i.e., basalt sand 14) to a surface 10 with an outer layer 12. In this example, outer layer 12 is first removed from surface 10 (FIG. 1A). Thereafter, basalt sand 14 is applied to surface 10 (FIG.1B) to form a new outer layer 16 on surface 10, which contains basalt sand 14 (FIG.1C). \|[0038] FIGS.2A-2B show an example of a more specific process to integrate an existing surface (i.e., a top sand 30 of a golf course) with a composition of the present disclosure (i.e., basalt sand 34) to build up a new outer layer 36 where basalt sands 34 are integrated in the top sand 30 of the greens and turf surface generally. As illustrated in FIG.2A, basalt sand 34 is applied to top sand 30 of a golf course with an outer layer (i.e., the grass and rootzone 32). In some embodiments, basalt sand 34 may be applied with agricultural spreaders, such as equipment 35, to top sand 30. As illustrated in FIG. 2B, the application of basalt sands 34 forms a new outer layer 36 on surface 30, which contains composition 34 integrated into surface 30 (FIG.2B). \|[0039] FIGS. 3A-3C show another specific method of integrating the compositions of the present disclosure (i.e., basalt sand 44) into a surface (i.e., a top sand 40 with topsoil 42) by using aeration as a chance to rapidly integrate larger amounts of basalt sands 44 deeper into the root zone of top sand 40. In this Example, equipment 43 is used to punch holes 45 into surface 40 of the grass. In some embodiments, such as process may remove around 10% of the organic matter dense root zone and topsoil 42 (FIGS.3A-3B). Thereafter, the same spreading equipment 43 may be used to backfill holes 45 with basalt sands 44 (FIGS. 3B-3C). This process is not only beneficial for managing organic matter in the surface and overall grass health, but also will allow basalt sands to penetrate deeper into the surface of the green. \|[0040] FIGS. 4A-4C show another specific method to integrate the compositions of the present disclosure (i.e., basalt sands 54) into a surface (i.e., top sand 50 with an outer layer 52). In this example, outer layer 52 is first removed from surface 50 (FIG.4A). Thereafter, composition 54 is applied to surface 50 (FIG.4B) to form a new outer layer 56 on surface 50, which contains composition 54 (FIG. 4C). In some embodiments, this option allows for a large amount of basalt sand to be used as the entire soil profile will be entirely rebuilt and basalt sands can be included in the blend as well as in the sand spread into the rootzone as the grass is regrown.\|[0041] The compositions of the present disclosure may be applied to a surface at various concentrations. For instance, in some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 0.1 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 0.5 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 1 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 2 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 2.5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 7.5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 10 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 25 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 50 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 75 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 100 tons per acre of the surface. \|[0042] The compositions of the present disclosure may be applied to a surface at varying levels of frequency. For instance, in some embodiments, the compositions of the present disclosure may be applied to a surface from one time to twenty times per year. In some embodiments, the compositions of the present disclosure may be applied to a surface from one time to five times per year. \|[0043] In some embodiments, full aeration and backfilling holes of a surface may only be done one to five times per year. Since a larger volume of soil may be removed through aeration, more top sand may be needed during aeration than regular top sanding.\|[0044] The compositions of the present disclosure may be applied to various surfaces. For instance, in some embodiments, the surface is associated with a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. \|[0045] In some embodiments, the field includes managed turf. In some embodiments, the managed turf is in the form of a monoculture. In some embodiments, the managed turf may require constant attention and maintenance as well as a high amount of nutrients and agricultural additives to keep the turf growing consistently. \|[0046] In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course, such as, but not exclusive to the accredited golf courses outlined in FIG.5. \|[0047] In some embodiments, the surface includes a soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0048] In some embodiments, the methods of the present disclosure also improve the quality of the soil. For instance, in some embodiments, the improved soil quality includes at least one of nutrient enhancement, enhanced CO2 capture, enhanced soil fertility, enhanced soil health, optimization of soil pH, or combinations thereof. As an example, soils developed on Holyoke Basalt as well as Blue ridge basalts have higher pH than those developed on surrounding rocks. They are also richer in nutrients, especially exchangeable Ca and Mg than soil. Table 2 compares soil pH, Organic Matter (OM) and cations on soils developed on north and south sides of ridges made of Holyoke Basalt in Massachusetts. Here, the concentrations are in ppm and uncertainties given in parentheses. The soils developed on Holyoke Basalt have low concentrations of heavy metals. Table 2. A comparison of soil pH, Organic Matter (OM) and cations on soils developed on north and south sides of ridges made of Holyoke Basalt in Massachusetts (data is from Karen B. Searcy, Brayton F. Wilson and James H. Fownes, The Journal of the Torrey Botanical Society, 2003, 130 (3), pp.158-169). \|[0049] In some embodiments, the improved soil quality provides various advantages. For instance, in some embodiments, the improved soil quality reduces or eliminates a need for the use of one or more soil nutrients, one or more soil fertilizers, additives (e.g., lime), or combinations thereof. \|[0050] Modified Surfaces \|[0051] Additional embodiments of the present disclosure pertain to modified surfaces. In some embodiments, the modified surfaces of the present disclosure include a composition of the present disclosure. Suitable compositions were described supra and are incorporated herein by reference.\|[0052] The compositions of the present disclosure may be associated with surfaces in various manners. For instance, in some embodiments, the compositions of the present disclosure are positioned on an outer layer of the surface. FIG.1C illustrates an example of a modified surface 20. In this example, modified surface 20 includes surface 10 with an outer layer 16 that contains a composition of the present disclosure 14. FIG.2B illustrates another example of a modified surface 39. In this example, modified surface 39 includes a surface 30 with an outer layer 36. In this example, a composition of the present disclosure 34 is integrated into surface 30 and outer layer 36. FIG.3C illustrates another example of a modified surface 49. In this example, modified surface 49 includes a surface 40 that contains a composition of the present disclosure 44 integrated into the surface. FIG. 4C illustrates another example of a modified surface 60. In this example, modified surface 60 includes a surface 50 with outer layer 56 that contains a composition of the present disclosure 54 integrated into the surface. \|[0053] The modified surfaces of the present disclosure may include various concentrations of the compositions of the present disclosure. For instance, in some embodiments, the composition is at a concentration of at least about 0.1 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 0.5 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 1 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 2 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 2.5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 7.5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 10 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 25 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 50 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 75 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 100 tons per acre of the surface.\|[0054] In some embodiments, the modified surfaces of the present disclosure are associated with a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course. \|[0055] In some embodiments, the modified surfaces of the present disclosure include a soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0056] In some embodiments, the composition improves the quality of the soil. For instance, in some embodiments, the improved soil quality includes at least one of nutrient enhancement, enhanced CO2 capture, enhanced soil fertility, enhanced soil health, optimization of soil pH, or combinations thereof. In some embodiments the improved soil quality reduces or eliminates a need for the use of one or more soil nutrients, one or more soil fertilizers, additives (e.g., lime), or combinations thereof. \|[0057] Methods of CO2 Capture from an Environment \|[0058] Additional embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment. In some embodiments, such methods include exposing the environment to a composition of the present disclosure. Suitable compositions were described supra and are incorporated herein by reference. In some embodiments, the basalt sands in the compositions of the present disclosure capture the CO2. \|[0059] The methods of the present disclosure may be utilized to capture CO2 from various environments. For instance, in some embodiments, the environment includes, without limitation, an airstream, a gas stream, an industrial plant, an atmosphere, ambient air, or combinations thereof. In some embodiments, the environment includes ambient air. \|[0060] Various methods may also be utilized to expose an environment to a composition of the present disclosure. For instance, in some embodiments, the exposing occurs by flowing the environment through the composition. In some embodiments, the exposing occurs by placing the composition at or near the environment.\|[0061] In some embodiments, the exposing occurs by applying the composition to a surface. Various methods may be utilized to apply the compositions of the present disclosure to a surface. For instance, in some embodiments, the application occurs by a method that includes, without limitation, spreading, pouring, sprinkling, spraying, or combinations thereof. \|[0062] In some embodiments, the methods of the present disclosure also include a step of removing an outer layer of a surface prior to applying the composition to the surface. In some embodiments, the composition is placed on an outer layer of the surface. \|[0063] The methods of the present disclosure may capture CO2 from various surfaces. For instance, in some embodiments the surface includes soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0064] In some embodiments, the surface includes a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course. \|[0065] The compositions of the present disclosure may be applied to surfaces at various concentrations for CO2 capture. For instance, in some embodiments, the composition is applied at a concentration of at least about 0.1 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 0.5 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 1 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 2 tons per acre of the surface per year. In some embodiments the composition is applied at a concentration of at least about 2.5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 7.5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 10 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 25 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 50 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 75 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 100 tons per acre of the surface. \|[0066] The methods of the present disclosure may be utilized to capture various types of CO2. For instance, in some embodiments, the captured CO2 includes atmospheric CO2. In some embodiments, the captured CO2 includes CO2 embedded within a surface. \|[0067] Without being bound by theory, CO2 capture may occur by various mechanisms. For instance, in some embodiments, CO2 capture may occur by at least one of sequestration, direct capture, adhesion, binding, adsorption, electrostatic interaction, or combinations thereof. \|[0068] Without being bound by further theory, CO2 capture may occur through various chemical reactions. For instance, in some embodiments, the CO2 capture occurs by a reaction between at least one basalt sand, CO2, and water. In some embodiments, the reaction releases one or more alkaline ions and mineralized bicarbonate (HCO3-). In some embodiments, the reactions combine HCO3- with Ca2+ ions to produce stable CaCO3 mineral.\|[0069] Without being bound by further theory, CO2 capture can occur through various reactions of silicate minerals, CO2, and H2O. For instance, in some embodiments where the basalt sand includesa CO2 capture reaction can occur through the reaction shown in equation 1.\|[0070] In some embodiments where the basalt sand includes NaAlSi3O8, a CO2 capture reaction can occur through the reaction shown in equation 2.\|[0071] In some embodiments where the basalt sand includes (Ca, Mg)2Si2O6, a CO2 capture reaction can occur through the reaction shown in equation 3.\|[0072] In some embodiments where the basalt sand includes (Mg, Fe)2SiO4, a CO2 capture reaction can occur through the reaction shown in equation 4.\|[0073] In some embodiments, atmospheric CO2 removed by a CO2 capture reaction is either retained as a long lived HCO3- or a CaCO3 precipitate. In some embodiments, production of these compounds leads to net removal of atmospheric CO2\|[0074] In some embodiments, Ca2+ and HCO3- react in accordance with equation 5 to result in the precipitation of CaCO3\|[0075] Methods of making basalt sand compositions \|[0076] Additional embodiments of the present disclosure pertain to methods of making the basalt sand compositions of the present disclosure. In some embodiments, such methods include crushing at least one basalt sand such that the crushing results in the formation of crushed basalt sand particles.\|[0077] In some embodiments, the methods of the present disclosure also include a step of isolating, filtering and/or drying the basalt sand. In some embodiments, the methods of the present disclosure include a step of filtering basalt sand based on the particle size of the basalt sand. In some embodiments, the isolating occurs prior to the crushing. In some embodiments, the isolating includes purifying at least one basalt sand. \|[0078] The methods of the present disclosure may be utilized to crush various basalt sands. Suitable basal sands were described supra and are incorporated herein by reference. For instance, in some embodiments, the basalt sands include, without limitation, plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. In some embodiments, at least one basalt sand includes a compound that includes, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4 or combinations thereof. \|[0079] Various methods may be utilized to crush basalt sands. For instance, in some embodiments, the crushing occurs by methods that include, without limitation, grinding, sonicating, pounding, compressing, milling (e.g., ball milling and/or hammer milling), or combinations thereof. In some embodiments, the crushed particles are in the form of fine-grained particles, course particles, medium particles, course-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. \|[0080] In some embodiments, the methods of the present disclosure also include a step of adding one or more additives to the basalt sand compositions. In some embodiments, the one or more additives include, without limitation, silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof. \|[0081] The methods of the present disclosure can have numerous embodiments. For instance, depending on the moisture content of the sands, kilns or other drying methods may be needed to produce spreadable top sand. \|[0082] Additional embodiments \|[0083] Reference will now be made to more specific embodiments of the present disclosure and experimental results that provide support for such embodiments. However, Applicants note that the disclosure below is for illustrative purposes only and is not intended to limit the scope of the claimed subject matter in any way.\|[0084] Example 1. Integrating Enhanced Rock Weathering (ERW) on Golf Courses \|[0085] This Example describes the deployment of enhanced rock weathering (ERW) practices alongside existing turf management programs to demonstrate the viability of ERW as a CO2 sequestration strategy for golf courses. This ERW strategy replaces traditional top sands with basalt sands for CO2 capture. \|[0086] Golf course construction typically entails a combination of subterranean drainage systems, irrigation, and the creation of an artificial topsoil consisting of a mixture of sand and soil to ensure proper drainage from the rootzone and base layer. In many cases, a “push-up green” is built with a custom blend of sand, peat moss (or other organic matter), and other additives. In some cases, a “sand- cap” is built over the existing sub-soil if the permeability is especially low. This is followed by layers of special soil, amended with sand to reduce the concentration of organic material (OM). An artificial topsoil may be necessary if the existing natural topsoil is too thin, lacking in nutrients, and/or over- compacted. Complete green construction guidelines are provided by the “USGA (2018). USGA Recommendations for a Method of Putting Green Construction.” \|[0087] After the topsoil has been created, seeding takes place and the “establishment period” begins. The grass begins to grow and root structures develop. \|[0088] Basalt sands could be integrated into existing golf course management programs. Moreover, when establishing a new course (or fully renovating an old course), designers can account for local conditions when integrating the basalt sands (e.g., climate, soil conditions, drainage, and/or local pests). \|[0089] Basalt sands could be used in laying the foundation for the entire course, incorporating many tons of crushed basalts into the sand-based root zone, and providing nutrient benefits to the surrounding soils and grasses. Additionally, fine-grained basalt sands could be used at multiple points in the development process with especially large quantities used during rootzone construction in addition to top sanding practices. Both cases provide an opportunity to integrate basalts effectively. \|[0090] The integration of basalt sands into the turf management programs at golf courses may bean optimal way to maximize the sequestration potential of golf courses. The highly managed soil structure of managed turf is ideally suited for enhanced rock weathering due to the high net primary productivity of the golf turf (estimated 1,100.5 g Carbon/m2/year), high volume of water flux from frequent irrigation, and existing systems for monitoring soil health, composition, and pH. (Wu, J., & Bauer, M. (2012). Estimating Net Primary Production of Turfgrass in an Urban-Suburban Landscape with QuickBird Imagery. Remote Sensing, Vol. 4, Issue 4, Pp. 849-866, 4, 849–866. https://doi.org/10.3390/rs4040849). \|[0091] This process has the potential to sequester an estimated 26 to 340 metric tons of carbon dioxide per golf course via green top and course wide sanding annually, depending on the integration level. With around 15,000 plus golf courses spread across the United States, this works out to an annual capture of between 391,000 and 5.15 million metric tons of CO2 per year from top dressing alone. \|[0092] These figures are calculated in Table 3. The sand application rates are derived from (Whitlark & Thompson, 2019; USGA Green Section Record, 57(9). https://www.usga.org/content/usga/home- page/course-care/green-section-record/57/9/light-and-frequent-topdressing-programs.html) and the sequestration rate of 20% is a rounded estimate based on current CDR potential figures from scientific literature, such as the basalts used in the Reershemius paper, which shows a capture potential of 183.56 kgCO2 t-1 (18.3%). This paper also discusses a potential method of measuring weathering based on a mass balance approach known as TiCAT. However, there are still questions regarding the effectiveness of this methodology (Reershemius, T., Kelland, M.E., Davis, I.R., D'Ascanio, R., Kalderon-Asael, B., Asael, D., Epihov, D.E., Beerling, D.J., Reinhard, C.T. and Planavsky, N.J., 2023. A new soil-based approach for empirical monitoring of enhanced rock weathering rates. arXiv preprint arXiv:2302.05004.). \|[0093] Additional simulations run on the MatLab weathering model from the Leverhulme Institute provided similar capture potential estimates of between 15-20% when parameters similar to that of a golf course soil profile were used. (Beerling et al., 2020, Nature, 583(7815), 242–248. https://doi.org/10.1038/s41586-020-2448-9; P. Renforth, 2012, International Journal of Greenhouse Gas Control, 10, 229–243). These estimates differ from the results in the lab experiment Applicants conducted using basalts from the Pioneer Valley.\|[0094] Regardless, in order to effectively measure and verify the amount of CO2 captured when basalt sands are deployed in the field, a reliable system of measurement must be developed. This verification process may include a variety of testing at individual courses. Various methods of measurement including, but not exclusive to, soil sampling, testing, other analyses, chemical testing, other laboratory or field-based testing, as well as sampling of water from existing drainage pipes and other sources around the course exist to conduct tests and analysis to verify weathering as well as the amount of CO2 sequestered. \|[0095] Tables 3-4 show the estimated values of carbon captured from golf courses. Calculations: Golf Course Annual Sand Use & CO2 Sequestration Potential EstimateCO2 Sequestration Tons/ Acre/ met. Tons/ hectare/ metric tons of Potential (metricTotal (Greens & Fairways – Combined)Table 3. Sand Use Estimates based on current industry top sand application rates and estimated CO2 Sequestration per golf course annual application. Table 4. Estimated range of value of Carbon Credits per golf course depending on the course integration level in USD($). \|[0096] The integration of basalt sands into the turf management practices of golf courses can be accomplished within existing infrastructure via putting green top sanding and aeration programs or through fairway top sanding. Although fairway top sanding and aeration is less common, recent golf turf grass studies emphasize the benefits of frequent and finer top sand applications to both greens and fairways. The adoption of course-wide top sanding significantly raises the sequestration opportunity to around 340 metric tons of CO2 per year. Depending on the course, basalt sands could also be used during construction or renovation to sequester greater amounts of CO2 once efficacy can be proven. \|[0097] To evaluate the extent to which alkalinity is released from basalt weathering, Applicants purchased rock powder Pioneer Valley basalt from Rock Dust Local (rockustlocal.com). This basalt is nearly identical in its chemical composition to that of Holyoke Basalt and has a maximum enhanced weathering CO2 capture potential of 203 kg CO2 t-1. The rock powder was dried and sieved. The particle size distribution of the rock power is shown in FIG.6.\|[0098] The basalt powder was mixed with sieved and dried soil from Dartmouth Organic Farm in a ratio of 10 g basalt to 170 g soil and packed in a Biorad® column to a height of ~6 cm. The soil used is Windsor loam. It is quite infertile and has not been fertilized. The column area is 23.76 cm2, meaning that the amount of basalt added is equivalent to 19 US ton/acre. As a control, 180 g of the same soil was also packed in columns as shown in FIG.7A. Water passed through the columns was weighed and measured for Na, K, Ca, and Mg. The alkalinity of the solution was also calculated. \|[0099] Experiments conducted over 3 months show that, with reference to the controls, the soil amended with basalt powder releases five-times more alkalinity (FIG. 7B). The data show that the basalt amended soil consumes 1.94 g of CO2 per 10 g of basalt (19.4% consumption) in comparison to soil control. This is equivalent to consumption of 194 kg of CO2 t-1 of basalt and approaches the theoretical maximum enhanced weathering CO2 capture potential for this rock. Additionally, the results are summarized in Table 5.Table 5. Changes in Alkalinity of effluent from basalt amended soil columns with reference to soil controls show that, on average, 19.4% of basalt was weathered over 88 days when 5 different elution experiments were conducted. Due to the time lag between experiments the total duration of experiments was about six months (May 2023-Oct 2023).\|[0100] While Applicants’ assessment of CO2 consumption per metric ton of basalt matches well with that recently reported experiment conducted over 4 years in an agricultural farm in Illinois (Beerling, D.J. et al. (2024) Enhanced weathering in the US Corn Belt delivers carbon removal with agronomic benefits, Proc. Nat. Acad. Sci.,121(9), e2319436121, https://doi.org/10.1073/pnas.2319436121), Applicants expect that the total CO2 consumed would be much higher in the golf courses, reaching the theoretical CO2 capture potential due to high temperatures and higher amounts of organic matter present in soil. \|[0101] Tables 6 and 7 provide general guidelines for top sands and USGA recommended root zones, respectively. Tables 6 and 7 provide recommended particle size distribution for a USGA approved Green rootzone construction, as well as a finer top sand blend that is based on the rootzone sand but with less coarse particles and more fine, ultra-fine, and other small particle sizes. A recent article (Whitlark & Thompson, 2019; USGA Green Section Record, 57(9). https://www.usga.org/content/usga/home-page/course-care/green-section-record/57/9/light-and- frequent-topdressing-programs.html) provided additional guidelines: “A general guideline is to select a sand that has a minimum of 50 percent of its particles in the medium-sized fraction (0.25-0.50 millimeters (mm) in diameter) and 15 to 40 percent in the coarse fraction (0.5-1.0 mm in diameter). The fine sand fraction (0.15-0.25 mm) should not exceed 25 percent, and the very fine fraction (0.05 – 0.15 mm) should not exceed 5 percent. Ideally, the material should have no particles greater than 1.0 mm in diameter given the difficulty in getting these larger particles to work down into the turf canopy. It is recommended to use a material with a coefficient of uniformity (CU) greater than 1.8. If the sand is too narrowly graded, which will produce a low CU, this may result in soft, unstable surfaces. However, the CU is not the only determining factor in stability – sand shape also plays a role, with angular sands being more stable. Utilizing a coarser sand during aeration will create more stability.” \|Typical Top sand GuidelinesTable 6. General guidelines for top sands.Table 7. General guidelines for USGA recommended root zones.\|[0102] Without further elaboration, it is believed that one skilled in the art can, using the description herein, utilize the present disclosure to its fullest extent. The embodiments described herein are to be construed as illustrative and not as constraining the remainder of the disclosure in any way whatsoever. While the embodiments have been shown and described, many variations and modifications thereof can be made by one skilled in the art without departing from the spirit and teachings of the invention. Accordingly, the scope of protection is not limited by the description set out above, but is only limited by the claims, including all equivalents of the subject matter of the claims. The disclosures of all patents, patent applications and publications cited herein are hereby incorporated herein by reference, to the extent that they provide procedural or other details consistent with and supplementary to those set forth herein.	(WO2024/186724)\| INTEGRATING ENHANCED ROCK WEATHERING AND TURF MANAGEMENT TO SEQUESTER ATMOSPHERIC CARBON DIOXIDE CROSS-REFERENCE TO RELATED APPLICATIONS \|[0001] The present application claims the benefit of U.S. Provisional Patent Application No. 63/449,791, filed on March 3, 2023. The entirety of the aforementioned application is incorporated herein by reference. BACKGROUND \|[0002] Current methods of capturing carbon dioxide (CO2) have numerous limitations in terms of efficacy, efficiency, costs, and the ability to capture CO2 at a large scale. Numerous embodiments of the present disclosure address the aforementioned limitations. SUMMARY \|[0003] In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand that is in the form of crushed particles. In some embodiments, the basalt sand is in purified form. In some embodiments, the basalt sand includes pre-treated basalt sand. In some embodiments, the basalt sand includes a plurality of different types of basalt sands. In some embodiments, the basalt sands of the present disclosure may be in the form of course particles, medium particles, course- grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. In some embodiments, the basalt sands may be mixed with other sands and/or soil additives. \|[0004] The basalt sands of the present disclosure may include various compounds. For instance, in some embodiments, the compounds may include, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof. In some embodiments, the basalt sand compositions of the present disclosure include, without limitation, plagioclase feldspars-containing basalt, pyroxenes-containing basalt, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof.\|[0005] Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. In some embodiments, the compositions of the present disclosure are placed on an outer layer of the surface. In some embodiments, the methods of the present disclosure may also include a step of removing an outer layer of a surface prior to applying a composition of the present disclosure to the surface. In some embodiments, the methods of the present disclosure also include a step of integrating the compositions of the present disclosure with a surface (e.g., within the topsoil and/or rootzone of a turf). \|[0006] Additional embodiments of the present disclosure pertain to modified surfaces that include a composition of the present disclosure. Further embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure. \|[0007] Additional embodiments of the present disclosure pertain to methods of making the basalt sand compositions of the present disclosure. In some embodiments, such methods include crushing at least one basalt sand such that the crushing results in the formation of crushed basalt sand particles. In some embodiments, the methods of the present disclosure also include a step of isolating, filtering, and/or drying the basalt sand. DESCRIPTION OF THE DRAWINGS \|[0008] FIGS. 1A-1C illustrate an exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a full rootzone basalt sand integration process. \|[0009] FIGS.2A-2B illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a top sand only basalt sand integration process. \|[0010] FIGS.3A-3C illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a basalt enhanced top sanding and aeration process, which can be used as part of ongoing aeration and top sanding programs to form a modified surface. \|[0011] FIGS.4A-4C illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a full rootzone basalt sand integration process.\|[0012] FIG.5 illustrates the locations of top 99 Golf Courses in the United States in relation to three major geologic provinces with basalt. \|[0013] FIG. 6 shows the particle size distribution of Pioneer Valley basalt from Rock Dust Local (rockustlocal.com). \|[0014] FIGS.7A-7B provide an experimental setup (FIG. 7A) and experimental results (FIG.7B) demonstrating that soil amended with basalt powder releases six-times more alkalinity than the control soil. DETAILED DESCRIPTION \|[0015] It is to be understood that both the foregoing general description and the following detailed description are illustrative and explanatory, and are not restrictive of the subject matter, as claimed. In this application, the use of the singular includes the plural, the word “a” or “an” means “at least one”, and the use of “or” means “and/or”, unless specifically stated otherwise. Furthermore, the use of the term “including”, as well as other forms, such as “includes” and “included”, is not limiting. Also, terms such as “element” or “component” encompass both elements or components comprising one unit and elements or components that include more than one unit unless specifically stated otherwise. \|[0016] The section headings used herein are for organizational purposes and are not to be construed as limiting the subject matter described. All documents, or portions of documents, cited in this application, including, but not limited to, patents, patent applications, articles, books, and treatises, are hereby expressly incorporated herein by reference in their entirety for any purpose. In the event that one or more of the incorporated literature and similar materials defines a term in a manner that contradicts the definition of that term in this application, this application controls. \|[0017] Climate change fundamentally threatens the safety and stability of modern civilization. In order to avoid the increasingly disastrous and costly effects of climate change, net atmospheric concentrations of greenhouse gases must be reduced. Such reductions can be achieved through improvements in productive efficiency (e.g., reducing CO2 emissions while maintaining output) and carbon dioxide (CO2) removal (CDR).\|[0018] Enhanced rock weathering (ERW) is an example of a CDR-based approach that aims to take atmospheric Carbon (CO2) out of air and store it as bicarbonate or carbonate. ERW has been investigated in cropland but not in golf courses or other managed turfs. Several different types of materials have been used for ERW, including peridotite, basalt, slag, and mine-tailings. Furthermore, ERW has beneficial effects on soil health by releasing beneficial mineral nutrients into the soil, such as calcium, potassium, phosphorous, and magnesium. \|[0019] However, ERW-based CDR processes utilizing peridotites, mine tailings, slag, and basalt other than tholeiites have numerous limitations. Foremost among them is the potential release of heavy metals to the environment and slow weathering kinetics. Furthermore, manufacturing large amounts of basalt powder (including mining, crushing, sorting, and shipping) can be an energy intensive process. Moreover, there is additional energy required to apply the basalt powder multiple times throughout the growing season with specialized spreading equipment that is typically gas powered. These costs and methods to spread the products for ERW would be especially difficult in places where this spreading is not common practice. This results in increased development costs and increased energy consumption. Such limitations may render ERW-based CDR processes inefficient and impractical for large scale CO2 capture from large surface areas. \|[0020] In comparison, golf course greens and courses at large, which, in general, are intensively managed, already engage in this top sanding process. They own and have the technical expertise to spread large amounts of sand onto the turf surface and rootzone. There are large amounts of research into turf grass and golf course maintenance practices aiding the development and deployment of basalt sands within existing maintenance and construction. Additionally, Golf courses have many characteristics that make them ideal to engender CDR through ERW as they are frequently located in warm and hot climates, are frequently watered and receive precipitation, and have high levels of primary productivity leading to turfs generating large amounts of organic matter—three parameters that increase the weathering rate. \|[0021] In sum, current methods of capturing CO2 have numerous limitations in terms of efficacy, efficiency, costs, and the ability to capture CO2 from large surface areas. Numerous embodiments of the present disclosure address the aforementioned limitations. \|[0022] Basalt sand compositions\|[0023] In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand. Basalt is the name of a mafic aphanitic volcanic rock that includes, without limitation, tholeiites. Basalt is exposed around the world on the continents and at the ocean floor. The basalt sands of the present disclosure may be in various forms. For instance, in some embodiments, the basalt sand is in isolated form (i.e., basalt sand isolated from its native environment). In some embodiments, the basalt sand is in the form of crushed particles. In some embodiments, the basalt sand is in purified form. In some embodiments, the basalt sand includes pre-treated basalt sand. In some embodiments, the basalt sands of the present disclosure may be in the form of course particles, medium particles, course-grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. \|[0024] The basalt sands of the present disclosure may include various compounds. For instance, in some embodiments, the compounds may include, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof. \|[0025] The compositions of the present disclosure may include various types of basalt sands. In some embodiments the basalt sand includes a plurality of different types of basalt sands. In some embodiments, the basalt sand includes, without limitation, plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. \|[0026] In some embodiments, the basalt sand compositions of the present disclosure include plagioclase feldspars-containing basalts and pyroxenes-containing basalts. In some embodiments, the basalt sand compositions of the present disclosure include microscopic or visible plagioclase feldspars-containing basalts and pyroxenes-containing basalts, with little or no olivines, and with minor iron spinel and phosphate. \|[0027] In some embodiments, the basalt sand compositions of the present disclosure include tholeiites. In some embodiments, the basalt sand compositions of the present disclosure include tholeiites with low heavy metal concentrations.\|[0028] In some embodiments, the basalt sand compositions of the present disclosure include Holyoke Basalt. In some embodiments, the Holyoke Basalt is derived from Massachusetts (MA). In some embodiments, the average concentrations of Cr, Ni, Cu, Zn, and Pb in Holyoke Basalt are 13 ppm, 33 ppm, 78 ppm, 86 ppm, and 4 ppm, respectively. In some embodiments, the average concentrations of Cr, Ni, Cu, Zn, and Pb in Holyoke Basalt are 384 ppm, 75 ppm, 145 ppm, 88 ppm, and 1.5 ppm, respectively. In some embodiments, Holyoke Basalt is essentially devoid of visible crystals. In some embodiments, Holyoke Basalt is in non-crystalline form. In some embodiments, Holyoke Basalt includes the following elements: SiO2, TiO2, Al2O3, Fe2O3, FeO, CaO, MgO, MnO, K2O, Na2O, and P2O5. \|[0029] In some embodiments, the basalt sand compositions of the present disclosure include Butner Basalt. In some embodiments, the Butner Basalt is derived from North Carolina (NC). In some embodiments, Butner Basalt is essentially devoid of visible crystals. In some embodiments, Butner Basalt is in non-crystalline form. \|[0030] In some embodiments, Holyoke Basalt and Butner Basalt each include the following elements: SiO2, TiO2, Al2O3, Fe2O3, FeO, CaO, MgO, MnO, K2O, Na2O, and P2O5. In some embodiments, the aforementioned elements are present at average weight percentages listed in Table 1. Table 1. Average weight percentages of major elements of Holyoke and Butner Basalts. The data are averages of published results downloaded from GEOROC.org. () FeO for Butner basalt reflects the total amount of iron present without making a distinction between Fe(II) and Fe(III). (*) EPOT is the maximum enhanced weathering CO2 capture potential in units of kg CO2 t-1 (as defined in Renforth (2019) The negative emission potential of alkaline materials. Nature Comm. https://doi.org/10.1038/s41467-019-09475-5). \|[0031] The basalt sands of the present disclosure may include various particle shapes. For instance, in some embodiments, the basalt sand particles of the present disclosure may be angular or rounded depending on their application. In some embodiments, different proportions of basalt sand particle sizes and blends may be used to best suit the local conditions. For instance, in some embodiments, finer sands may retain more moisture within an upper rootzone of a soil. In some embodiments, such sands may also include reduced moisture content through various treatment methods (e.g., kiln drying) so that they can be applied to a surface more effectively (e.g., more efficient spreading using golf course sand spreading and aeration equipment). \|[0032] The compositions of the present disclosure may also include additional components. For instance, in some embodiments, the compositions of the present disclosure may also include one or more additives. In some embodiments, the one or more additives include, without limitation, silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz- based top sands, lime, or combinations thereof.\|[0033] In some embodiments, the additives include one or more golf course additives. In some embodiments, the golf course additives include, without limitation, peat moss, quartz-based top sands, lime, or combinations thereof. In some embodiments, the quartz-based top sands are utilized to dilute the basalt. In some embodiments, the basalt sand compositions of the present disclosure may be treated with such additives depending on the needs of a surface (e.g., a local soil). \|[0034] Methods of modifying a surface \|[0035] Additional embodiments of the present disclosure pertain to methods of modifying a surface. In some embodiments, such methods include applying a composition of the present disclosure to the surface. Suitable compositions were described supra and are incorporated herein by reference. \|[0036] The compositions of the present disclosure may be applied to surfaces in various manners. For instance, in some embodiments, the compositions of the present disclosure may be applied by methods that include, without limitation, spreading, pouring, sprinkling, spraying, or combinations thereof. In some embodiments, the compositions of the present disclosure are placed on an outer layer of the surface. In some embodiments, the compositions of the present disclosure may become integrated with the surface. In some embodiments, the methods of the present disclosure may also include a step of removing an outer layer of a surface prior to applying a composition of the present disclosure to the surface. \|[0037] FIGS. 1A-1C, 2A-2B, 3A-3C, and 4A-4C illustrate exemplary processes for applying a composition of the present disclosure to a surface. For instance, FIGS.1A-1C illustrate an exemplary process for applying a composition of the present disclosure (i.e., basalt sand 14) to a surface 10 with an outer layer 12. In this example, outer layer 12 is first removed from surface 10 (FIG. 1A). Thereafter, basalt sand 14 is applied to surface 10 (FIG.1B) to form a new outer layer 16 on surface 10, which contains basalt sand 14 (FIG.1C). \|[0038] FIGS.2A-2B show an example of a more specific process to integrate an existing surface (i.e., a top sand 30 of a golf course) with a composition of the present disclosure (i.e., basalt sand 34) to build up a new outer layer 36 where basalt sands 34 are integrated in the top sand 30 of the greens and turf surface generally. As illustrated in FIG.2A, basalt sand 34 is applied to top sand 30 of a golf course with an outer layer (i.e., the grass and rootzone 32). In some embodiments, basalt sand 34 may be applied with agricultural spreaders, such as equipment 35, to top sand 30. As illustrated in FIG. 2B, the application of basalt sands 34 forms a new outer layer 36 on surface 30, which contains composition 34 integrated into surface 30 (FIG.2B). \|[0039] FIGS. 3A-3C show another specific method of integrating the compositions of the present disclosure (i.e., basalt sand 44) into a surface (i.e., a top sand 40 with topsoil 42) by using aeration as a chance to rapidly integrate larger amounts of basalt sands 44 deeper into the root zone of top sand 40. In this Example, equipment 43 is used to punch holes 45 into surface 40 of the grass. In some embodiments, such as process may remove around 10% of the organic matter dense root zone and topsoil 42 (FIGS.3A-3B). Thereafter, the same spreading equipment 43 may be used to backfill holes 45 with basalt sands 44 (FIGS. 3B-3C). This process is not only beneficial for managing organic matter in the surface and overall grass health, but also will allow basalt sands to penetrate deeper into the surface of the green. \|[0040] FIGS. 4A-4C show another specific method to integrate the compositions of the present disclosure (i.e., basalt sands 54) into a surface (i.e., top sand 50 with an outer layer 52). In this example, outer layer 52 is first removed from surface 50 (FIG.4A). Thereafter, composition 54 is applied to surface 50 (FIG.4B) to form a new outer layer 56 on surface 50, which contains composition 54 (FIG. 4C). In some embodiments, this option allows for a large amount of basalt sand to be used as the entire soil profile will be entirely rebuilt and basalt sands can be included in the blend as well as in the sand spread into the rootzone as the grass is regrown.\|[0041] The compositions of the present disclosure may be applied to a surface at various concentrations. For instance, in some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 0.1 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 0.5 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 1 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 2 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 2.5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 7.5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 10 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 25 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 50 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 75 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 100 tons per acre of the surface. \|[0042] The compositions of the present disclosure may be applied to a surface at varying levels of frequency. For instance, in some embodiments, the compositions of the present disclosure may be applied to a surface from one time to twenty times per year. In some embodiments, the compositions of the present disclosure may be applied to a surface from one time to five times per year. \|[0043] In some embodiments, full aeration and backfilling holes of a surface may only be done one to five times per year. Since a larger volume of soil may be removed through aeration, more top sand may be needed during aeration than regular top sanding.\|[0044] The compositions of the present disclosure may be applied to various surfaces. For instance, in some embodiments, the surface is associated with a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. \|[0045] In some embodiments, the field includes managed turf. In some embodiments, the managed turf is in the form of a monoculture. In some embodiments, the managed turf may require constant attention and maintenance as well as a high amount of nutrients and agricultural additives to keep the turf growing consistently. \|[0046] In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course, such as, but not exclusive to the accredited golf courses outlined in FIG.5. \|[0047] In some embodiments, the surface includes a soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0048] In some embodiments, the methods of the present disclosure also improve the quality of the soil. For instance, in some embodiments, the improved soil quality includes at least one of nutrient enhancement, enhanced CO2 capture, enhanced soil fertility, enhanced soil health, optimization of soil pH, or combinations thereof. As an example, soils developed on Holyoke Basalt as well as Blue ridge basalts have higher pH than those developed on surrounding rocks. They are also richer in nutrients, especially exchangeable Ca and Mg than soil. Table 2 compares soil pH, Organic Matter (OM) and cations on soils developed on north and south sides of ridges made of Holyoke Basalt in Massachusetts. Here, the concentrations are in ppm and uncertainties given in parentheses. The soils developed on Holyoke Basalt have low concentrations of heavy metals. Table 2. A comparison of soil pH, Organic Matter (OM) and cations on soils developed on north and south sides of ridges made of Holyoke Basalt in Massachusetts (data is from Karen B. Searcy, Brayton F. Wilson and James H. Fownes, The Journal of the Torrey Botanical Society, 2003, 130 (3), pp.158-169). \|[0049] In some embodiments, the improved soil quality provides various advantages. For instance, in some embodiments, the improved soil quality reduces or eliminates a need for the use of one or more soil nutrients, one or more soil fertilizers, additives (e.g., lime), or combinations thereof. \|[0050] Modified Surfaces \|[0051] Additional embodiments of the present disclosure pertain to modified surfaces. In some embodiments, the modified surfaces of the present disclosure include a composition of the present disclosure. Suitable compositions were described supra and are incorporated herein by reference.\|[0052] The compositions of the present disclosure may be associated with surfaces in various manners. For instance, in some embodiments, the compositions of the present disclosure are positioned on an outer layer of the surface. FIG.1C illustrates an example of a modified surface 20. In this example, modified surface 20 includes surface 10 with an outer layer 16 that contains a composition of the present disclosure 14. FIG.2B illustrates another example of a modified surface 39. In this example, modified surface 39 includes a surface 30 with an outer layer 36. In this example, a composition of the present disclosure 34 is integrated into surface 30 and outer layer 36. FIG.3C illustrates another example of a modified surface 49. In this example, modified surface 49 includes a surface 40 that contains a composition of the present disclosure 44 integrated into the surface. FIG. 4C illustrates another example of a modified surface 60. In this example, modified surface 60 includes a surface 50 with outer layer 56 that contains a composition of the present disclosure 54 integrated into the surface. \|[0053] The modified surfaces of the present disclosure may include various concentrations of the compositions of the present disclosure. For instance, in some embodiments, the composition is at a concentration of at least about 0.1 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 0.5 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 1 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 2 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 2.5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 7.5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 10 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 25 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 50 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 75 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 100 tons per acre of the surface.\|[0054] In some embodiments, the modified surfaces of the present disclosure are associated with a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course. \|[0055] In some embodiments, the modified surfaces of the present disclosure include a soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0056] In some embodiments, the composition improves the quality of the soil. For instance, in some embodiments, the improved soil quality includes at least one of nutrient enhancement, enhanced CO2 capture, enhanced soil fertility, enhanced soil health, optimization of soil pH, or combinations thereof. In some embodiments the improved soil quality reduces or eliminates a need for the use of one or more soil nutrients, one or more soil fertilizers, additives (e.g., lime), or combinations thereof. \|[0057] Methods of CO2 Capture from an Environment \|[0058] Additional embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment. In some embodiments, such methods include exposing the environment to a composition of the present disclosure. Suitable compositions were described supra and are incorporated herein by reference. In some embodiments, the basalt sands in the compositions of the present disclosure capture the CO2. \|[0059] The methods of the present disclosure may be utilized to capture CO2 from various environments. For instance, in some embodiments, the environment includes, without limitation, an airstream, a gas stream, an industrial plant, an atmosphere, ambient air, or combinations thereof. In some embodiments, the environment includes ambient air. \|[0060] Various methods may also be utilized to expose an environment to a composition of the present disclosure. For instance, in some embodiments, the exposing occurs by flowing the environment through the composition. In some embodiments, the exposing occurs by placing the composition at or near the environment.\|[0061] In some embodiments, the exposing occurs by applying the composition to a surface. Various methods may be utilized to apply the compositions of the present disclosure to a surface. For instance, in some embodiments, the application occurs by a method that includes, without limitation, spreading, pouring, sprinkling, spraying, or combinations thereof. \|[0062] In some embodiments, the methods of the present disclosure also include a step of removing an outer layer of a surface prior to applying the composition to the surface. In some embodiments, the composition is placed on an outer layer of the surface. \|[0063] The methods of the present disclosure may capture CO2 from various surfaces. For instance, in some embodiments the surface includes soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0064] In some embodiments, the surface includes a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course. \|[0065] The compositions of the present disclosure may be applied to surfaces at various concentrations for CO2 capture. For instance, in some embodiments, the composition is applied at a concentration of at least about 0.1 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 0.5 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 1 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 2 tons per acre of the surface per year. In some embodiments the composition is applied at a concentration of at least about 2.5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 7.5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 10 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 25 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 50 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 75 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 100 tons per acre of the surface. \|[0066] The methods of the present disclosure may be utilized to capture various types of CO2. For instance, in some embodiments, the captured CO2 includes atmospheric CO2. In some embodiments, the captured CO2 includes CO2 embedded within a surface. \|[0067] Without being bound by theory, CO2 capture may occur by various mechanisms. For instance, in some embodiments, CO2 capture may occur by at least one of sequestration, direct capture, adhesion, binding, adsorption, electrostatic interaction, or combinations thereof. \|[0068] Without being bound by further theory, CO2 capture may occur through various chemical reactions. For instance, in some embodiments, the CO2 capture occurs by a reaction between at least one basalt sand, CO2, and water. In some embodiments, the reaction releases one or more alkaline ions and mineralized bicarbonate (HCO3-). In some embodiments, the reactions combine HCO3- with Ca2+ ions to produce stable CaCO3 mineral.\|[0069] Without being bound by further theory, CO2 capture can occur through various reactions of silicate minerals, CO2, and H2O. For instance, in some embodiments where the basalt sand includesa CO2 capture reaction can occur through the reaction shown in equation 1.\|[0070] In some embodiments where the basalt sand includes NaAlSi3O8, a CO2 capture reaction can occur through the reaction shown in equation 2.\|[0071] In some embodiments where the basalt sand includes (Ca, Mg)2Si2O6, a CO2 capture reaction can occur through the reaction shown in equation 3.\|[0072] In some embodiments where the basalt sand includes (Mg, Fe)2SiO4, a CO2 capture reaction can occur through the reaction shown in equation 4.\|[0073] In some embodiments, atmospheric CO2 removed by a CO2 capture reaction is either retained as a long lived HCO3- or a CaCO3 precipitate. In some embodiments, production of these compounds leads to net removal of atmospheric CO2\|[0074] In some embodiments, Ca2+ and HCO3- react in accordance with equation 5 to result in the precipitation of CaCO3\|[0075] Methods of making basalt sand compositions \|[0076] Additional embodiments of the present disclosure pertain to methods of making the basalt sand compositions of the present disclosure. In some embodiments, such methods include crushing at least one basalt sand such that the crushing results in the formation of crushed basalt sand particles.\|[0077] In some embodiments, the methods of the present disclosure also include a step of isolating, filtering and/or drying the basalt sand. In some embodiments, the methods of the present disclosure include a step of filtering basalt sand based on the particle size of the basalt sand. In some embodiments, the isolating occurs prior to the crushing. In some embodiments, the isolating includes purifying at least one basalt sand. \|[0078] The methods of the present disclosure may be utilized to crush various basalt sands. Suitable basal sands were described supra and are incorporated herein by reference. For instance, in some embodiments, the basalt sands include, without limitation, plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. In some embodiments, at least one basalt sand includes a compound that includes, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4 or combinations thereof. \|[0079] Various methods may be utilized to crush basalt sands. For instance, in some embodiments, the crushing occurs by methods that include, without limitation, grinding, sonicating, pounding, compressing, milling (e.g., ball milling and/or hammer milling), or combinations thereof. In some embodiments, the crushed particles are in the form of fine-grained particles, course particles, medium particles, course-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. \|[0080] In some embodiments, the methods of the present disclosure also include a step of adding one or more additives to the basalt sand compositions. In some embodiments, the one or more additives include, without limitation, silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof. \|[0081] The methods of the present disclosure can have numerous embodiments. For instance, depending on the moisture content of the sands, kilns or other drying methods may be needed to produce spreadable top sand. \|[0082] Additional embodiments \|[0083] Reference will now be made to more specific embodiments of the present disclosure and experimental results that provide support for such embodiments. However, Applicants note that the disclosure below is for illustrative purposes only and is not intended to limit the scope of the claimed subject matter in any way.\|[0084] Example 1. Integrating Enhanced Rock Weathering (ERW) on Golf Courses \|[0085] This Example describes the deployment of enhanced rock weathering (ERW) practices alongside existing turf management programs to demonstrate the viability of ERW as a CO2 sequestration strategy for golf courses. This ERW strategy replaces traditional top sands with basalt sands for CO2 capture. \|[0086] Golf course construction typically entails a combination of subterranean drainage systems, irrigation, and the creation of an artificial topsoil consisting of a mixture of sand and soil to ensure proper drainage from the rootzone and base layer. In many cases, a “push-up green” is built with a custom blend of sand, peat moss (or other organic matter), and other additives. In some cases, a “sand- cap” is built over the existing sub-soil if the permeability is especially low. This is followed by layers of special soil, amended with sand to reduce the concentration of organic material (OM). An artificial topsoil may be necessary if the existing natural topsoil is too thin, lacking in nutrients, and/or over- compacted. Complete green construction guidelines are provided by the “USGA (2018). USGA Recommendations for a Method of Putting Green Construction.” \|[0087] After the topsoil has been created, seeding takes place and the “establishment period” begins. The grass begins to grow and root structures develop. \|[0088] Basalt sands could be integrated into existing golf course management programs. Moreover, when establishing a new course (or fully renovating an old course), designers can account for local conditions when integrating the basalt sands (e.g., climate, soil conditions, drainage, and/or local pests). \|[0089] Basalt sands could be used in laying the foundation for the entire course, incorporating many tons of crushed basalts into the sand-based root zone, and providing nutrient benefits to the surrounding soils and grasses. Additionally, fine-grained basalt sands could be used at multiple points in the development process with especially large quantities used during rootzone construction in addition to top sanding practices. Both cases provide an opportunity to integrate basalts effectively. \|[0090] The integration of basalt sands into the turf management programs at golf courses may bean optimal way to maximize the sequestration potential of golf courses. The highly managed soil structure of managed turf is ideally suited for enhanced rock weathering due to the high net primary productivity of the golf turf (estimated 1,100.5 g Carbon/m2/year), high volume of water flux from frequent irrigation, and existing systems for monitoring soil health, composition, and pH. (Wu, J., & Bauer, M. (2012). Estimating Net Primary Production of Turfgrass in an Urban-Suburban Landscape with QuickBird Imagery. Remote Sensing, Vol. 4, Issue 4, Pp. 849-866, 4, 849–866. https://doi.org/10.3390/rs4040849). \|[0091] This process has the potential to sequester an estimated 26 to 340 metric tons of carbon dioxide per golf course via green top and course wide sanding annually, depending on the integration level. With around 15,000 plus golf courses spread across the United States, this works out to an annual capture of between 391,000 and 5.15 million metric tons of CO2 per year from top dressing alone. \|[0092] These figures are calculated in Table 3. The sand application rates are derived from (Whitlark & Thompson, 2019; USGA Green Section Record, 57(9). https://www.usga.org/content/usga/home- page/course-care/green-section-record/57/9/light-and-frequent-topdressing-programs.html) and the sequestration rate of 20% is a rounded estimate based on current CDR potential figures from scientific literature, such as the basalts used in the Reershemius paper, which shows a capture potential of 183.56 kgCO2 t-1 (18.3%). This paper also discusses a potential method of measuring weathering based on a mass balance approach known as TiCAT. However, there are still questions regarding the effectiveness of this methodology (Reershemius, T., Kelland, M.E., Davis, I.R., D'Ascanio, R., Kalderon-Asael, B., Asael, D., Epihov, D.E., Beerling, D.J., Reinhard, C.T. and Planavsky, N.J., 2023. A new soil-based approach for empirical monitoring of enhanced rock weathering rates. arXiv preprint arXiv:2302.05004.). \|[0093] Additional simulations run on the MatLab weathering model from the Leverhulme Institute provided similar capture potential estimates of between 15-20% when parameters similar to that of a golf course soil profile were used. (Beerling et al., 2020, Nature, 583(7815), 242–248. https://doi.org/10.1038/s41586-020-2448-9; P. Renforth, 2012, International Journal of Greenhouse Gas Control, 10, 229–243). These estimates differ from the results in the lab experiment Applicants conducted using basalts from the Pioneer Valley.\|[0094] Regardless, in order to effectively measure and verify the amount of CO2 captured when basalt sands are deployed in the field, a reliable system of measurement must be developed. This verification process may include a variety of testing at individual courses. Various methods of measurement including, but not exclusive to, soil sampling, testing, other analyses, chemical testing, other laboratory or field-based testing, as well as sampling of water from existing drainage pipes and other sources around the course exist to conduct tests and analysis to verify weathering as well as the amount of CO2 sequestered. \|[0095] Tables 3-4 show the estimated values of carbon captured from golf courses. Calculations: Golf Course Annual Sand Use & CO2 Sequestration Potential EstimateCO2 Sequestration Tons/ Acre/ met. Tons/ hectare/ metric tons of Potential (metricTotal (Greens & Fairways – Combined)Table 3. Sand Use Estimates based on current industry top sand application rates and estimated CO2 Sequestration per golf course annual application. Table 4. Estimated range of value of Carbon Credits per golf course depending on the course integration level in USD($). \|[0096] The integration of basalt sands into the turf management practices of golf courses can be accomplished within existing infrastructure via putting green top sanding and aeration programs or through fairway top sanding. Although fairway top sanding and aeration is less common, recent golf turf grass studies emphasize the benefits of frequent and finer top sand applications to both greens and fairways. The adoption of course-wide top sanding significantly raises the sequestration opportunity to around 340 metric tons of CO2 per year. Depending on the course, basalt sands could also be used during construction or renovation to sequester greater amounts of CO2 once efficacy can be proven. \|[0097] To evaluate the extent to which alkalinity is released from basalt weathering, Applicants purchased rock powder Pioneer Valley basalt from Rock Dust Local (rockustlocal.com). This basalt is nearly identical in its chemical composition to that of Holyoke Basalt and has a maximum enhanced weathering CO2 capture potential of 203 kg CO2 t-1. The rock powder was dried and sieved. The particle size distribution of the rock power is shown in FIG.6.\|[0098] The basalt powder was mixed with sieved and dried soil from Dartmouth Organic Farm in a ratio of 10 g basalt to 170 g soil and packed in a Biorad® column to a height of ~6 cm. The soil used is Windsor loam. It is quite infertile and has not been fertilized. The column area is 23.76 cm2, meaning that the amount of basalt added is equivalent to 19 US ton/acre. As a control, 180 g of the same soil was also packed in columns as shown in FIG.7A. Water passed through the columns was weighed and measured for Na, K, Ca, and Mg. The alkalinity of the solution was also calculated. \|[0099] Experiments conducted over 3 months show that, with reference to the controls, the soil amended with basalt powder releases five-times more alkalinity (FIG. 7B). The data show that the basalt amended soil consumes 1.94 g of CO2 per 10 g of basalt (19.4% consumption) in comparison to soil control. This is equivalent to consumption of 194 kg of CO2 t-1 of basalt and approaches the theoretical maximum enhanced weathering CO2 capture potential for this rock. Additionally, the results are summarized in Table 5.Table 5. Changes in Alkalinity of effluent from basalt amended soil columns with reference to soil controls show that, on average, 19.4% of basalt was weathered over 88 days when 5 different elution experiments were conducted. Due to the time lag between experiments the total duration of experiments was about six months (May 2023-Oct 2023).\|[0100] While Applicants’ assessment of CO2 consumption per metric ton of basalt matches well with that recently reported experiment conducted over 4 years in an agricultural farm in Illinois (Beerling, D.J. et al. (2024) Enhanced weathering in the US Corn Belt delivers carbon removal with agronomic benefits, Proc. Nat. Acad. Sci.,121(9), e2319436121, https://doi.org/10.1073/pnas.2319436121), Applicants expect that the total CO2 consumed would be much higher in the golf courses, reaching the theoretical CO2 capture potential due to high temperatures and higher amounts of organic matter present in soil. \|[0101] Tables 6 and 7 provide general guidelines for top sands and USGA recommended root zones, respectively. Tables 6 and 7 provide recommended particle size distribution for a USGA approved Green rootzone construction, as well as a finer top sand blend that is based on the rootzone sand but with less coarse particles and more fine, ultra-fine, and other small particle sizes. A recent article (Whitlark & Thompson, 2019; USGA Green Section Record, 57(9). https://www.usga.org/content/usga/home-page/course-care/green-section-record/57/9/light-and- frequent-topdressing-programs.html) provided additional guidelines: “A general guideline is to select a sand that has a minimum of 50 percent of its particles in the medium-sized fraction (0.25-0.50 millimeters (mm) in diameter) and 15 to 40 percent in the coarse fraction (0.5-1.0 mm in diameter). The fine sand fraction (0.15-0.25 mm) should not exceed 25 percent, and the very fine fraction (0.05 – 0.15 mm) should not exceed 5 percent. Ideally, the material should have no particles greater than 1.0 mm in diameter given the difficulty in getting these larger particles to work down into the turf canopy. It is recommended to use a material with a coefficient of uniformity (CU) greater than 1.8. If the sand is too narrowly graded, which will produce a low CU, this may result in soft, unstable surfaces. However, the CU is not the only determining factor in stability – sand shape also plays a role, with angular sands being more stable. Utilizing a coarser sand during aeration will create more stability.” \|Typical Top sand GuidelinesTable 6. General guidelines for top sands.Table 7. General guidelines for USGA recommended root zones.\|[0102] Without further elaboration, it is believed that one skilled in the art can, using the description herein, utilize the present disclosure to its fullest extent. The embodiments described herein are to be construed as illustrative and not as constraining the remainder of the disclosure in any way whatsoever. While the embodiments have been shown and described, many variations and modifications thereof can be made by one skilled in the art without departing from the spirit and teachings of the invention. Accordingly, the scope of protection is not limited by the description set out above, but is only limited by the claims, including all equivalents of the subject matter of the claims. The disclosures of all patents, patent applications and publications cited herein are hereby incorporated herein by reference, to the extent that they provide procedural or other details consistent with and supplementary to those set forth herein.	Family Number\|(111402698)\|111402698\|Abstract\|(WO2024186724 A1)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.\|(AU2024233973 A1)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.(From WO2024186724 A1)\|(KR20250164234 A)\|Embodiments of the present disclosure are directed to compositions comprising at least one basalt sand in the form of crushed particles. A further embodiment of the present disclosure is directed to a method of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure are directed to modified surfaces comprising compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from the environment by exposing the environment to the compositions of the present disclosure, and methods of making basalt sand compositions of the present disclosure.\|(EP4676898 A1)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.\|(JP2026510743 A)\| The present invention relates to a composition containing at least one type of basalt sand in the form of crushed particles. A further embodiment of the disclosure relates to a method for modifying a surface by a step of applying the composition to the surface. Further embodiments of the disclosure relate to a modified surface containing the composition of the disclosure, a method for capturing carbon dioxide (CO2) from the environment by a step of bringing the environment into contact with the composition of the disclosure, and a method for preparing the basalt sand composition of the disclosure. Selected View Figure 2\|Title\|(WO2024186724 A1)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide\|(AU2024233973 A1)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide\|(KR20250164234 A)\|Integration of strengthening rock weathering and lawn management to isolate carbon dioxide in the atmosphere\|(CA3288102 A1)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide\|(EP4676898 A1)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide\|(JP2026510743 A)\|Integration of rock weathering acceleration and turf management to sequester atmospheric carbon dioxide\|Independent Claims\|(WO2024186724 A1)\|1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt (...) \|(AU2024233973 A1)\|1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt sand captures (...) \|(KR20250164234 A)\|1. A method of capturing carbon dioxide (CO2) from an environment, the method comprising exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt (...) \|(JP2026510743 A)\|1. A method for capturing carbon dioxide (CO2) from the environment, which comprises a step of bringing the environment into contact with a composition, wherein the composition is The method comprises at least one kind of pulverized Basalt sand, and CO2 (...) \|	Chemical engineering\|Environmental technology\|Materials, metallurgy\|Other special machines	A01G-020/20\|B01D-053/62\|B01D-2257/504\|C04B-014/14\|C04B-022/10\|C04B-030/00\|C04B-2111/00019\|Y02C-020/40	(GR1) C04B-030/00[RK1]; C04B-014/14[RK2]; C04B-022/10[RK3]	A01G-020/20\|B01D-053/62\|B01D-2257/504\|C04B-014/14\|C04B-022/10\|C04B-030/00\|C04B-2111/00019\|Y02C-020/40	A01G-009/033\|A01G-020/00\|A01G-020/10\|A01G-020/20\|B01D-053/14\|B01D-053/62\|B01J-020/10\|C01B-033/24\|C01B-033/26\|C04B-014/04\|C04B-014/14\|C04B-022/10\|C04B-028/26\|C04B-030/00\|C04B-035/20\|C04B-111/00	A01G-009/033\|A01G-020/00\|A01G-020/10\|A01G-020/20\|B01D-053/14\|B01D-053/62\|B01J-020/10\|C01B-033/24\|C01B-033/26\|C04B-014/04\|C04B-014/14\|C04B-022/10\|C04B-028/26\|C04B-030/00\|C04B-035/20\|C04B-111/00					WO2022200450\|EP-826298	WO2022200450 101953667 WHO=Examiner SELF=N CAT=X CAT=Y\|EP-826298 573750 WHO=Examiner SELF=N CAT=X CAT=Y		WO2022200450; XP037187522; EP-826298; XP093211151\|\|\|\|\|	\|(WO2024/186724)\|International Search Report [Examiner]\|-BEERLING DAVID J.; KANTZAS EURIPIDES P.; LOMAS MARK R.; WADE PETER; EUFRASIO RAFAEL M.; RENFORTH PHIL; SARKAR BINOY; ANDREWS M. GR: "Potential for large-scale COremoval via enhanced rock weathering with croplands", NATURE, vol. 583, no. 7815, 8 July 2020 (2020-07-08), pages 242 - 248, XP037187522, DOI: 10.1038/s41586-020-2448-9\|-CHANG CHUNG CHIN: "A GRAVITY STUDY OF THE TRIASSIC VALLEY IN SOUTHERN CONNECTICUT", ECONOMIC AND ENVIRONMENTAL GEOLOGY, vol. 2, no. 2, 30 June 1969 (1969-06-30), XP093211151, ISSN: 1225-7281\|\|\|\|\|	PENDING	(EP4676898)\|PENDING\|(WO2024/186724)\|PENDING\|(JP2026510743)\|PENDING\|(KR10-2025-0164234)\|PENDING\|(AU2024233973)\|PENDING\|(CA3288102)\|PENDING	ALIVE	(EP4676898)\|ALIVE\|(WO2024/186724)\|ALIVE\|(JP2026510743)\|ALIVE\|(KR10-2025-0164234)\|ALIVE\|(AU2024233973)\|ALIVE\|(CA3288102)\|ALIVE	(EP4676898)\|LEGAL DETAILS FOR EP4676898\|Actual or expected expiration date=2044-03-04\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-04\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP 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events\|Application details\|Application country=CA CA3288102\|Application date=2024-03-04\|Standardized application number=2024CA-3288102\|Event publication date=2024-09-12\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA3288102\|Publication stage code=A1\|Publication date=2024-09-12\|Standardized publication number=CA3288102	(EP4676898)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4676898)\|Extension States: BA\|(EP4676898)\|Validation States: MA, MD, TN, KH, GE\|(WO2024/186724)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2024/186724)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2024/186724)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2024/186724)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2024/186724)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP4676898)\|EP\|(WO2024/186724)\|WO; AU; CA; EP; JP; KR\|(JP2026510743)\|JP\|(KR10-2025-0164234)\|KR\|(AU2024233973)\|AU\|(CA3288102)\|CA	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=iCBy9VOVqJVSDVsa5jTXaqCa4vFyxJplNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006578671&ekey=2380&xpn=EP4676898&kind=A1	https://register.epo.org/application?number=EP24767679	https://permalink.orbit.com/RenderStaticFirstPage?XPN=NfY8daI1uDcbWDK85JFymXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2024/186724)\|US	(WO2024/186724)\|NAME=TRUSTEES OF DARTMOUTH COLLEGE 11 Rope Ferry Road, #6210 Hanover, NH 03755-1404 , COUNTRY=US	(EP4676898)\|DE\|(WO2024/186724)\|US\|\|\|(AU2024233973)\|AU\|(CA3288102)\|CA	(EP4676898)\|NAME=Maiwald GmbH;Engineering Elisenhof Elisenstrasse 3 , CITY=80335 München , COUNTRY=DE , REG=101782373\|(WO2024/186724)\|NAME=AMINI, Farhang Shackelford, Bowen, McKinley & Norton, LLP 717 Texas Avenue, Suite 2700 Houston, TX 77002 , POSTCODE=77002 , COUNTRY=US\|(JP2026510743)\|NAME=YAMAMOTO Osamu , REG=100118902NAME=MIYAMAE,Toru , REG=100106208NAME=MATSUO JUNICHI , REG=100196508NAME=NAKAMURA MITSUTOSHI , REG=100126985\|(KR10-2025-0164234)\|NAME=KIM, JIN HOI NAME=KIM, TAE HONG\|(AU2024233973)\|NAME=PHILLIPS ORMONDE FITZPATRICK PO Box 24171 , CITY=Melbourne , STATE=VIC , POSTCODE=3001 , COUNTRY=AU\|(CA3288102)\|NAME=MBM INTELLECTUAL PROPERTY AGENCY 275 SLATER STREET, 14TH FLOOR , CITY=OTTAWA , POSTCODE=K1P 5H9 , COUNTRY=CA , REG=e61a1630-b292-4706-b91c-f3098c8c5df7	(EP4676898)\|US; US\|(WO2024/186724)\|US; US\|\|\|\|(CA3288102)\|US; US	(EP4676898)\|NAME=SHARMA, Mukul, CITY=Hanover, NH 03755-1404, COUNTRY=US \|NAME=MORRISON, Brian, CITY=Miami, FL 33156, COUNTRY=US\|(WO2024/186724)\|NAME=SHARMA, Mukul c/o Trustees of Dartmouth College 11 Rope Ferry Road, #6210 Hanover, NH 03755-1404, POSTCODE=03755-1404, COUNTRY=US \|NAME=MORRISON, Brian 7245 S.W. 125th Street Miami, FL 33156, POSTCODE=33156, COUNTRY=US\|(JP2026510743)\|NAME=Sharma, Mukuru\|(KR10-2025-0164234)\|NAME=MORRISON BRIAN\|NAME=SHARMA MUKUL\|(AU2024233973)\|NAME=MORRISON, Brian\|NAME=SHARMA, Mukul\|(CA3288102)\|NAME=MORRISON Brian 7245 S.W. 125th Street, CITY=Miami, POSTCODE=33156, STATE=FL , COUNTRY=US \|NAME=SHARMA Mukul c/o Trustees of Dartmouth College 11 Rope Ferry Road, #6210, CITY=Hanover, POSTCODE=03755-1404, STATE=NH , COUNTRY=US	(WO2024/186724)\|7\|(JP2026510743)\|7\|(KR10-2025-0164234)\|7\|(AU2024233973)\|7	2	6			(EP4676898)\|WO2024/186724\|(JP2026510743)\|WO2024/186724\|(KR10-2025-0164234)\|WO2024/186724\|(AU2024233973)\|WO2024/186724\|(CA3288102)\|WO2024/186724		(WO2024/186724)\|Number of Claims: NCL=54\|Extended kind: EXTK=x\|\|(JP2026510743)\|Number of Claims: NCL=54\|Request for examination: REQEXA=false\|\|(KR10-2025-0164234)\|Number of Claims: NCL=54\|\|(AU2024233973)\|Number of Claims: NCL=54\|		(EP4676898)\|ENGLISH (ENG)	(JP2026510743)\|Patent\|(EP4676898)\|Patent\|(KR20250164234)\|Patent\|(AU2024233973)\|Patent\|(CA3288102)\|Patent\|(WO2024186724)\|Patent	Titre: (EP4676898)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide Résumé: (EP4676898)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.	14	Abstract	gpt-4o-mini	yes	The article discusses methods for capturing CO₂ using basalt sand, which is a silicate mineral, and focuses on enhanced rock weathering for carbon sequestration.
18	US63/638,100P\|US19/186,905	WOCA2025/050589\|US19/186,905	US20250333914\|WO2025/222295	116414688	WO2025/222295 A1 2025-10-30 [WO2025222295]\|US20250333914 A1 2025-10-30 [US20250333914]	2024-04-24\|2025-04-23	2025-04-23\|2025-04-23	2025-10-30\|2025-10-30		(US20250333914)\|2045-04-23\|(WO2025/222295)\|2027-10-24	(US20250333914)\|Carbon capture system and method for synthetic turf fields	(US20250333914)\|A synthetic turf system including a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes rock dust, or the synthetic turf system further includes a layer of the rock dust disposed above or below the one or more infill layers. The rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.	TARKETT SPORTS	(US20250333914)\|Tarkett Sports Canada Inc. ([CA])\|(WO2025/222295)\|TARKETT SPORTS CANADA INC. ([CA])	SMOLLETT JASON\|HABIB ERIC\|CHISAM CHRISTOPHER	(US20250333914)\|Smollett Jason\|Habib Eric\|Chisam Christopher	(WO2025/222295)\|YIP, Vincent ([CA])	(US20250333914)\|Furthermore, it will be appreciated that by placing the rock dust 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air.\|It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the rock dust 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-7 are intended solely as one non-limiting example of turf carpet systems in which the rock dust 102 may be utilized.\|	(US20250333914)\|1. A synthetic turf system comprising: a backing; turf fibers extended upward from the backing; and one or more infill layers positioned above the backing, below a top portion of the turf fibers, wherein the one or more infill layers includes rock dust, or the synthetic turf system further comprises a layer of the rock dust disposed above or below the one or more infill layers, and the rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.\|14. Infill for a synthetic turf system, the infill comprising: rock dust including silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, wherein at least 90 percent of the rock dust has a particle size less than 250 micrometers in diameter; and organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust in one or more infill layers.\|17. A method of preparing a synthetic turf system, the method comprising: dispersing rock dust over a top portion of turf fibers, wherein the rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|	(US20250333914)\|As used in this application, "or" is intended to mean an inclusive "or" rather than an exclusive "or".\|In accordance with some aspects described herein, there is provided an synthetic turf system that utilizes a material derived from one or more types of rock dust, including, for example and without limitation, basalt rock dust, igneous rock dust (such as andesite, diorite, gabbro, or rhyolite), limestone-derived dust (such as calcium carbonate-based materials), dolomitic lime (CaO/MgO), ultramafic rock dust (such as peridotite or dunite), industrial byproducts containing reactive silicates or carbonates, a blend of various types of rock dust, combinations thereof, or other similar mineral-based particulate materials.\|In yet another aspect, a layer of rock dust-based particles may be positioned on a geotextile or subgrade layer.\|	(US20250333914)\|ROCK DUST(100,77)\|SYNTHETIC TURF FIELD(100,3)\|CARBON CAPTURE(100,2)\|TURF FIBER(73,32)\|INFILL LAYER(72,54)\|SILICATE ROCK(66,14)\|ROCK REACTION(58,13)\|SYNTHETIC TURF(54,62)\|ROCK DUST INCORPORATION(52,1)\|ROCK DUST PLACEMENT(46,1)\|RAINWATER(42,29)\|BACKING(39,28)\|LIMESTONE DERIVED DUST(39,1)\|IGNEOUS ROCK(38,11)\|ULTRAMAFIC ROCK DUST(38,1)\|BASE ROCK LAYER(37,46)\|IGNEOUS ROCK DUST(36,1)\|ELASTOMER PARTICLE(34,5)\|THERMOPLASTIC PARTICLE(33,5)\|DISPERSING ROCK(33,2)\|SILICATE REACTION(33,1)\|ROCK DUST PARTICLE(32,3)\|LAYERED INSTALLATION(32,1)\|ROCK DUST PARTICLE LAYER(32,1)\|BICARBONATE(31,11)\|DUST(30,9)\|ROCK(27,53)\|DOLOMITIC LIME(27,4)\|RUBBER PARTICLE(26,5)\|PERIDOTITE(26,4)\|ANDESITE(25,4)\|RHYOLITE(25,4)\|BYPRODUCT(25,1)\|DIORITE(24,4)\|AMERICAN SOCIETY(24,1)\|SUBGRADE LAYER(24,1)\|SYNTHETIC TURF BACKING(24,1)\|COATED PARTICLE(23,5)\|DUNITE(23,4)\|ANDTHE(23,2)\|GEOTEXTILE(23,1)\|SYNTHETIC TURF INFILL LAYER(23,1)\|BASALT(22,5)\|ORGANIC PARTICLE(22,5)\|WEATHERED PARTICLE(22,2)\|ANDONE(22,1)\|TURF(22,1)\|INFILL(21,6)\|DUST PARTICLE(21,5)\|GEOTEXTILE COMPONENT(20,10)\|SUBGRADE(18,10)\|WOLLASTONITE(18,4)\|QUICKLIME(18,3)\|INCH EIGHTH(17,2)\|MINERAL PARTICULATE MATERIAL(17,1)\|BLEND(15,1)\|SPHERICITY(13,3)\|CALCIUM CARBONATE MATERIAL(13,1)\|INFILL LAYER THICKNESS(12,2)\|ORTHE(12,1)\|ASTM(11,4)\|CARBONATE MATERIAL(11,1)\|GROUND(10,3)\|SHOCK PAD(8,6)\|BICARBONATE SUBSTANCE(8,4)\|TOP DRESSING(8,3)\|PARTICLE SIZE(7,7)\|CARBONATE SEDIMENT(7,2)\|WENTWORTH AGGREGATE CLASSIFICATION(7,1)\|DRAINAGE PIPE(6,2)\|ROCK DUST REACTION(6,2)\|AERIAL SPREADER(6,1)\|ARTIFICIAL TURF INFILL(6,1)\|BALLAST INFILL(6,1)\|COMPACTION VARIABILITY(6,1)\|CONJOINED CLAUSE(6,1)\|ENGINEERED DRAINAGE(6,1)\|HANDHELD SPREADER(6,1)\|LAYMOR BRUSH(6,1)\|MESH SIZE(6,1)\|PERMEABLE SUBGRADE(6,1)\|PROPYLENE DIENE MONOMER(6,1)\|TURF BRUSHING EQUIPMENT(6,1)\|CARBON DIOXIDE(5,10)\|BROADCASTER TOOL(5,1)\|ENDPOINT RECITATION(5,1)\|IMPERMEABLE BARRIER(5,1)\|OSCILLATING BRUSH(5,1)\|PARTICLE SIZING(5,1)\|PERMEABLE BACKING(5,1)\|PNEUMATIC SPREADER(5,1)\|ROCK COMPACTION(5,1)\|ROCK DUST MIXING(5,1)\|SANDY SOILS(5,1)\|SEED TENDER(5,1)\|STONE DISPERSION(5,1)\|STORM DRAIN OUTLET(5,1)\|WALK BEHIND ROTARY BRUSH(5,1)\|CARBONIC ACID(4,7)\|INFILL MATERIAL(4,6)\|CARPET(4,3)\|STORM WATER(4,3)\|ULTRAMAFIC ROCK(4,3)\|DEACIDIFYING(4,2)\|HOPPER GATE(4,2)\|AIR BOOM SPREADER(4,1)\|BALL INTERACTION(4,1)\|DRAINAGE ELEVATION(4,1)\|GEOTEXTILE FABRIC LAYER(4,1)\|HYDRAULIC BRUSH(4,1)\|NATURAL BYPRODUCT(4,1)\|RAINWATER POOLING FLOW(4,1)\|ROCK BLEND(4,1)\|SUBDRAIN TRENCH BOTTOM(4,1)\|SYNTHETIC TURF INSTALLATION(4,1)\|TRIANGULAR BRUSH(4,1)\|ROCK DUST LAYER(3,9)\|NOMINAL SIZE RANGE(3,4)\|RIVER(3,4)\|SEA(3,4)\|DOLOMITE(3,2)\|HYDRAULICALLY CONTROLLED CONVEYER(3,2)\|MINERAL NUTRIENT(3,2)\|OLIVINE(3,2)\|THERMOPLASTIC(3,2)\|TRACTION(3,2)\|COMPACTED STONE BASE(3,1)\|DESCRIPTOR(3,1)\|FLEXIBLE BRUSH(3,1)\|INFILL LAYER LAYERED ARRANGEMENT(3,1)\|MODIFIED SUBGRADE(3,1)\|PACKING STABILITY(3,1)\|PARTICLE ETHYLENE(3,1)\|RAIN WATER REACTION(3,1)\|RIGID BRUSH(3,1)\|ROCK DUST COMPOSITIONAL RANGE(3,1)\|ROTARY BRUSH ACTION(3,1)\|STRAIGHT BRUSH(3,1)\|\|(WO2025/222295)\|ROCK DUST(100,80)\|SYNTHETIC TURF FIELD(100,4)\|CARBON CAPTURE(100,3)\|TURF FIBER(77,32)\|INFILL LAYER(74,54)\|SILICATE ROCK(65,14)\|ROCK REACTION(57,13)\|SUBDRAIN TRENCH(54,5)\|SYNTHETIC TURF(53,62)\|ROCK DUST INCORPORATION(51,1)\|BACKING(47,28)\|ROCK DUST PLACEMENT(45,1)\|RAINWATER(41,29)\|GEOTEXTILE FABRIC(40,1)\|IGNEOUS ROCK(38,11)\|BASE ROCK LAYER(37,46)\|GEOTEXTILE FABRIC LAYER(34,1)\|ELASTOMER PARTICLE(33,5)\|DISPERSING ROCK(33,2)\|THERMOPLASTIC PARTICLE(32,5)\|ROCK DUST PARTICLE(32,3)\|LAYERED INSTALLATION(31,1)\|ROCK DUST PARTICLE LAYER(31,1)\|BICARBONATE(30,11)\|SUBDRAIN TRENCH BOTTOM(30,1)\|INFILL(27,7)\|RUBBER PARTICLE(25,5)\|ROCK(24,53)\|AMERICAN SOCIETY(23,1)\|GEOTEXTILE(23,1)\|SUBGRADE LAYER(23,1)\|SYNTHETIC TURF BACKING(23,1)\|SYNTHETIC TURF INFILL LAYER(23,1)\|COATED PARTICLE(22,5)\|ORGANIC PARTICLE(22,5)\|WEATHERED PARTICLE(22,2)\|ENVIRONMENTALLY FRIENDLY(22,1)\|TURF(22,1)\|DUST PARTICLE(21,5)\|TRANSPORTATION(21,1)\|GEOTEXTILE COMPONENT(20,10)\|DUST(18,6)\|QUICKLIME(18,3)\|DOLOMITIC LIME(17,4)\|PERIDOTITE(17,4)\|WOLLASTONITE(17,4)\|ANDESITE(16,4)\|DIORITE(16,4)\|RHYOLITE(16,4)\|INCH EIGHTH(16,2)\|ROCK DUST MATERIAL(16,1)\|DUNITE(15,4)\|BASALT(14,5)\|SPHERICITY(12,3)\|INFILL LAYER THICKNESS(12,2)\|ASTM(11,4)\|CARBON NEUTRAL(11,1)\|DUST MATERIAL(11,1)\|SHOCK PAD(8,6)\|BICARBONATE SUBSTANCE(8,4)\|CARBON OFFSETTING MATERIAL(8,1)\|PARTICLE SIZE(7,7)\|TOP DRESSING(7,3)\|CARBONATE SEDIMENT(7,2)\|MECHANICAL RESISTANCE(7,1)\|WENTWORTH AGGREGATE CLASSIFICATION(7,1)\|MECHANICAL PROPERTY(6,3)\|DRAINAGE PIPE(6,2)\|ROCK DUST REACTION(6,2)\|CONJOINED CLAUSE(6,1)\|AERIAL SPREADER(5,1)\|ARTIFICIAL TURF INFILL(5,1)\|BALLAST INFILL(5,1)\|BROADCASTER TOOL(5,1)\|COMPACTION VARIABILITY(5,1)\|ENDPOINT RECITATION(5,1)\|ENGINEERED DRAINAGE(5,1)\|HANDHELD SPREADER(5,1)\|IMPERMEABLE BARRIER(5,1)\|LAYMOR BRUSH(5,1)\|LIMESTONE DERIVED DUST(5,1)\|MESH SIZE(5,1)\|OSCILLATING BRUSH(5,1)\|PARTICLE SIZING(5,1)\|PERMEABLE BACKING(5,1)\|PERMEABLE SUBGRADE(5,1)\|PNEUMATIC SPREADER(5,1)\|PROPYLENE DIENE MONOMER(5,1)\|ROCK COMPACTION(5,1)\|ROCK DUST MIXING(5,1)\|SANDY SOILS(5,1)\|SEED TENDER(5,1)\|STONE DISPERSION(5,1)\|STORM DRAIN OUTLET(5,1)\|TURF BRUSHING EQUIPMENT(5,1)\|ULTRAMAFIC ROCK DUST(5,1)\|WALK BEHIND ROTARY BRUSH(5,1)\|CARBONIC ACID(4,7)\|INFILL MATERIAL(4,6)\|STORM WATER(4,3)\|DEACIDIFYING(4,2)\|HOPPER GATE(4,2)\|AIR BOOM SPREADER(4,1)\|BALL INTERACTION(4,1)\|DRAINAGE ELEVATION(4,1)\|HIGH AVAILABILITY(4,1)\|HYDRAULIC BRUSH(4,1)\|IGNEOUS ROCK DUST(4,1)\|NATURAL BYPRODUCT(4,1)\|RAINWATER POOLING FLOW(4,1)\|ROCK BLEND(4,1)\|SILICATE REACTION(4,1)\|SYNTHETIC TURF INSTALLATION(4,1)\|TRIANGULAR BRUSH(4,1)\|ROCK DUST LAYER(3,9)\|NOMINAL SIZE RANGE(3,4)\|RIVER(3,4)\|SEA(3,4)\|CARPET(3,3)\|DOLOMITE(3,2)\|HYDRAULICALLY CONTROLLED CONVEYER(3,2)\|MINERAL NUTRIENT(3,2)\|OLIVINE(3,2)\|THERMOPLASTIC(3,2)\|TRACTION(3,2)\|COMPACTED STONE BASE(3,1)\|DESCRIPTOR(3,1)\|FLEXIBLE BRUSH(3,1)\|INFILL LAYER LAYERED ARRANGEMENT(3,1)\|MODIFIED SUBGRADE(3,1)\|PACKING STABILITY(3,1)\|PARTICLE ETHYLENE(3,1)\|RAIN WATER REACTION(3,1)\|RIGID BRUSH(3,1)\|ROCK DUST COMPOSITIONAL RANGE(3,1)\|ROTARY BRUSH ACTION(3,1)\|STRAIGHT BRUSH(3,1)\|SYNTHETIC TURF MANUFACTURING(3,1)\|	(US20250333914)\|1. A synthetic turf system comprising:\| a backing;\| turf fibers extended upward from the backing; and\| one or more infill layers positioned above the backing, below a top portion of the turf fibers, wherein the one or more infill layers includes rock dust, or the synthetic turf system further comprises a layer of the rock dust disposed above or below the one or more infill layers, and\| the rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.\|2. The synthetic turf system of claim 1, wherein the rock dust includes wollastonite, basalt, peridotite, dunite, dolomitic lime, dolostone, andesite, diorite, gabbro, rhyolite, quick lime, or lime stone.\|3. The synthetic turf system of claim 1, wherein the rock dust includes silicate rock, igneous rock, or reactive rock.\|4. The synthetic turf system of claim 3, wherein the silicate rock, igneous rock, or reactive rock forms weathered particles having a sphericity of about 0.65 to about 0.85.\|5. The synthetic turf system of claim 1, further comprising a base stone layer disposed below the backing, and the rock dust is layered above, layered below, or mixed in the base stone layer.\|6. The synthetic turf system of claim 5, wherein the base stone layer is a first base stone layer formed from stone having a first nominal size range,\| the system further comprises a second base stone layer disposed below the first base stone layer, the second base stone layer having a second nominal size range coarser than the first nominal size range, and\| the rock dust is layered above, layered below, or mixed in the second base stone layer.\|7. The synthetic turf system of claim 6, wherein the first base stone layer is at least one inch thick and formed from American Society for Testing and Materials (ASTM) #89 stone, and the second base stone layer is at least 2 inches thick and formed from ASTM #57 stone.\|8. The synthetic turf system of claim 5, wherein the backing and the base stone layer are water permeable, and the rock dust is accessible by rainwater traveling through the one or more infill layers by gravity.\|9. The synthetic turf system of claim 5, wherein the base stone layer includes silicate rock, igneous rock, or reactive rock that is accessible to rainwater traveling from the top portion of the turf fibers by gravity.\|10. The synthetic turf system of claim 5, wherein the rock dust is layered directly on a top surface of the base stone layer, the rock dust forming a layer with a thickness of at least one eighth of an inch, or\| the rock dust is layered below a geotextile component, the rock dust forming a layer with a thickness of at least half an inch, the geotextile component being disposed underneath the base stone layer,\| the rock dust is tilled into a subgrade below the base stone layer, or\| the rock dust is positioned in a subdrain below the base stone layer.\|11. The synthetic turf system of claim 1, further comprising a subdrain trench below the backing, wherein the rock dust is blended with stone in the subdrain trench.\|12. The synthetic turf system of claim 1, wherein at least ninety percent of the rock dust has a particle size less than 62 micrometers in diameter.\|13. The synthetic turf system of claim 1, wherein the one or more infill layers include the rock dust, the one or more infill layers are disposed on top of the backing, between the turf fibers, and the top portion of the turf fibers extends above the one or more infill layers.\|14. Infill for a synthetic turf system, the infill comprising:\| rock dust including silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, wherein at least 90 percent of the rock dust has a particle size less than 250 micrometers in diameter; and\| organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust in one or more infill layers.\|15. The infill of claim 14, wherein the rock dust forms less than 10 percent of the infill by weight and includes wollastonite, basalt, peridotite, dunite, dolomitic lime, dolostone, andesite, diorite, gabbro, rhyolite, quick lime, or lime stone.\|16. The infill of claim 14, wherein 90 percent of the rock dust by weight has a particle size of 4 to 125 micrometers in diameter.\|17. A method of preparing a synthetic turf system, the method comprising:\| dispersing rock dust over a top portion of turf fibers, wherein the rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|18. The method of claim 17, further comprising:\| grooming the rock dust into the one or more infill layers of the synthetic turf system, between the turf fibers, at a backing of the synthetic turf system.\|19. The method of claim 17, further comprising:\| preblending the silicate rock, igneous rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the rock dust over the top portion of the turf fibers.\|20. The method of claim 17, further comprising:\| measuring an aspect of the synthetic turf system, including a thickness of an infill layer, an acidity of rainwater at the infill layer, or a quantity of silicate rock, igneous rock, or reactive rock present in the infill layer; and\| dispersing a predetermined quantity of the rock dust over the top portion of the turf fibers as a top dressing based on the measured aspect.	(US20250333914)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] The application claims priority to and the benefit of U.S. Provisional Patent Application No. 63/638,100, filed on Apr. 24, 2024, entitled “Carbon Capture System and Method for Synthetic Turf Fields”, which we incorporate by reference in its entirety.\|(US20250333914)\|BACKGROUND\|[0002] Synthetic or artificial turf fields are composed of three primary components—from bottom to top: Shock pad, carpet, and infill. These components are generally assembled on top of a base of compacted stone. The shock pad is optional and serves to convey much of the shock absorption performance of the turf field, required for the safety of those playing on the surface in the case of impact with the surface. The carpet serves to mimic the blades of grass and root zone, conveying the softness and traction of the surface as well as many of the ball interaction properties. The infill is generally constituted of at least two layers, the bottom layer of which serves to weight down and stabilize the carpets that it is laid onto, whereas the top layers serve as an additional interface layer to those playing on the field, conveying surface softness, friction, traction, and much of the mechanical properties of the field that are felt directly by the players.\|[0003] When installation of a synthetic turf field occurs, generally speaking, a living, natural turf field is being replaced with an artificial one. In this process, a living organism, e.g., grass, plants, etc., which naturally removes carbon dioxide from the atmosphere is removed. Additionally, the construction associated with a synthetic turf field, as well as the actual manufacturing of the synthetic turf, result in additional carbon entering the atmosphere.\|SUMMARY\|[0004] The following presents a simplified summary to provide a basic understanding of some aspects of the disclosed subject matter. This summary is not an extensive overview. It is not intended to identify key/critical elements or to delineate the scope of the claimed subject matter. Its sole purpose is to present some concepts in a simplified form as a prelude to the more detailed description presented later.\|[0005] There remains a need for environmentally friendly and ultimately carbon-neutral or carbon-offsetting materials that present good mechanical properties and mechanical resistance, while presenting high availability, easy transportation, and low cost.\|[0006] In aspects, a rock dust-based layer may be positioned immediately below the installation of an synthetic turf system, e.g., below a shock pad, on a top substrate material, e.g., a rock layer. In such a position, the rock dust-based layer may have a thickness of ⅛″ to ¼″.\|[0007] In still other aspects, rock dust-based particles may be blended into a 1″ to 2″ topping stone layer positioned immediately below the shock pad.\|[0008] In yet another aspect, a layer of rock dust-based particles may be positioned on a geotextile or subgrade layer. In such a position, the rock dust-based layer may have a thickness of ¼″ to ½″.\|[0009] In another aspect, a rock dust-based material may be positioned at a bottom of a subdrain trench, below a layer of geotextile fabric.\|[0010] In a further aspect, rock dust-based particles may be tilled or blended into native subgrade material. In such a position, the rock dust-based particles may be blended within the subgrade, e.g., soil, as discussed below.\|[0011] In another aspect, a synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes rock dust, or the synthetic turf system further includes a layer of the rock dust disposed above or below the one or more infill layers. The rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.\|[0012] In another aspect, infill for a synthetic turf system includes rock dust. The rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater. At least 90 percent of the rock dust has a particle size less than 250 micrometers. Organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust in one or more infill layers.\|[0013] In another aspect, a method of preparing a synthetic turf system includes dispersing rock dust over a top portion of turf fibers. The rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|[0014] In each of the foregoing aspects, certain carbon sequestration processes can occur as rainwater interacts with the rock dust-based particles, regardless of the position in the synthetic turf system. Further discussion of the processes referenced above are included in the following description.\|[0015] To the accomplishment of the foregoing and related ends, certain illustrative aspects of the claimed subject matter are described herein in connection with the following description and the annexed drawings. These aspects indicate various ways in which the subject matter may be practiced, all of which are intended to be within the scope of the disclosed subject matter. Other advantages and novel features may become apparent from the following detailed description when considered in conjunction with the drawings.\|[0016] These and other systems, methods, objects, features, and advantages of the present disclosure will be apparent to those skilled in the art from the following detailed description of the preferred embodiment and the drawings.\|[0017] All documents mentioned herein are hereby incorporated in their entirety by reference. References to items in the singular should be understood to include items in the plural, and vice versa, unless explicitly stated otherwise or clear from the text. Grammatical conjunctions are intended to express any and all disjunctive and conjunctive combinations of conjoined clauses, sentences, words, and the like, unless otherwise stated or clear from the context.\|(US20250333914)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] FIG. 1 is a partial perspective view of an example synthetic turf system having an infill made of rock dust in accordance with some embodiments of the present disclosure.\|[0019] FIG. 2 is a perspective view of an example application system employed in dispersing the rock dust over the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0020] FIG. 3 is a perspective view of an example brush employed in grooming the rock dust into the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0021] FIG. 4 is a partial perspective view of an example synthetic turf system having rock dust applied to a top surface of a base stone layer in accordance with some embodiments.\|[0022] FIG. 5 is a partial perspective view of an example synthetic turf system having rock dust incorporated into a base stone layer in accordance with some embodiments.\|[0023] FIG. 6 is a partial perspective view of an example synthetic turf system having the rock dust positioned on a geotextile component in accordance with some embodiments.\|[0024] FIG. 7 is a partial perspective view of an example synthetic turf system having rock dust positioned in a subdrain trench in accordance with some embodiments.\|[0025] FIG. 8 is a partial perspective view of an example synthetic turf system having rock dust diffused into a subgrade in accordance with some embodiments.\|[0026] FIG. 9 is an example process flow for preparing a synthetic turf system.\|(US20250333914)\|DETAILED DESCRIPTION\|[0027] Various aspects of the subject disclosure are now described in more detail with reference to the annexed drawings, wherein like numerals generally refer to like or corresponding elements throughout. It should be understood, however, that the drawings and detailed description relating thereto are not intended to limit the claimed subject matter to the particular form disclosed. Instead, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the described and claimed subject matter.\|[0028] The following disclosure provides many different embodiments, or examples, for implementing different features of the provided subject matter. Specific examples of components and arrangements are described below to simplify the present disclosure. These are, of course, merely examples and are not intended to be limiting. For example, the formation of a first feature over or on a second feature in the description that follows may include embodiments in which the first and second features are formed in direct contact, and may also include embodiments in which additional features may be formed between the first and second features, such that the first and second features may not be in direct contact. In addition, the present disclosure may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.\|[0029] Further, spatially relative terms, such as “beneath,” “below,” “lower,” “above,” “upper” and the like, may be used herein for ease of description to describe one element or feature's relationship to another element(s) or feature(s) as illustrated in the figures. The spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. The apparatus may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein may likewise be interpreted accordingly.\|[0030] Numerical values in the specification and claims of this application should be understood to include numerical values which are the same when reduced to the same number of significant figures and numerical values which differ from the stated value by less than the experimental error of conventional measurement technique of the type described in the present application to determine the value. All ranges disclosed herein are inclusive of the recited endpoint.\|[0031] The term “about” can be used to include any numerical value that can vary without changing the basic function of that value. When used with a range, “about” also discloses the range defined by the absolute values of the two endpoints, e.g., “about 2 to about 4” also discloses the range “from 2 to 4.” For example, the term “about” may refer to plus or minus 10% of the indicated number.\|[0032] In accordance with some aspects described herein, there is provided an synthetic turf system that utilizes a material derived from one or more types of rock dust, including, for example and without limitation, basalt rock dust, igneous rock dust (such as andesite, diorite, gabbro, or rhyolite), limestone-derived dust (such as calcium carbonate-based materials), dolomitic lime (CaO/MgO), ultramafic rock dust (such as peridotite or dunite), industrial byproducts containing reactive silicates or carbonates, a blend of various types of rock dust, combinations thereof, or other similar mineral-based particulate materials. In some embodiments, the rock dust may be used as an intervening layer of material between existing layers of the system, mixed within a particular layer, lining a subdrain trench, on or mixed within a substrate, or combinations thereof. It will further be appreciated that as the rock dust is a natural byproduct of the mining industry, there is no additional carbon footprint from mining.\|[0033] In some embodiments contemplated herein, the rock dust material, when in contact with rainwater, causes a chemical reaction to occur between carbonic acid naturally present in the rainwater and the rock dust. The reaction weathers the rock dust and converts the carbonic acid into a carbonate or bicarbonate. By converting the carbon dioxide into other substances, the carbon dioxide can no longer be released into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These carbonate or bicarbonate substances are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments. These carbonate sediments form a sink for carbon dioxide.\|[0034] Turning now to FIG. 1, there is shown a three-dimensional cross-sectional view of a portion of an synthetic turf system 100 utilizing rock dust 102 for carbon sequestration in accordance with an example implementation of the embodiment described above. As shown in FIG. 1, the synthetic turf system 100 includes one or more infill layers 104, a backing 110, and a plurality of turf fibers 112 that emulate grass blades extending substantially perpendicularly upwards relative to the backing 110. As such, the infill layers 104 are positioned above the backing 110, in between the turf fibers 112, and below a top portion 114 of the turf fibers 112.\|[0035] Infill, as shown in FIG. 1, is representative of material that is deposited directly on top of the backing 110 and forms the infill layers 104 around the turf fibers 112. Infill is interspersed between the turf fibers 112, rising out of the backing 110. As depicted, the infill layers 104 have a total depth that covers a portion of the turf fibers 112, leaving at least part of the top portion 114 exposed and extending above the infill layers 104.\|[0036] In accordance with some embodiments, the infill layers 104 assist in supporting the turf fibers 112 in an upright position from the backing 110, and provide traction and shock absorption. As a general matter, various types of infill arrangements are contemplated. In this regard, the one or more infill layers 104 may be a single homogeneous or graded layer, or a plurality of distinct layers. For example, two layer, three layer, or other further layered arrangements of the one or more infill layers 104 are contemplated. For convenience, the present description primarily discusses two and three layer embodiments.\|[0037] In some embodiments, a first layer 120 of infill material may include, for example and without limitation, styrene-butadiene rubber (SBR) particles ethylene propylene diene monomer (EPDM) rubber, other thermoplastics such as polyvinyl chloride (PVC), composite materials can be used that combine thermoplastics, elastomers, reinforcements and/or fillers or other sufficient material, is incorporated. In accordance with some embodiments, a second layer 122 of infill material depicted in FIG. 1 may include a mixture of materials, e.g., material of the first layer 104 and a sand material. In such embodiments, a third layer 124 of infill material may include the aforementioned sand material, which may be implemented as a ballast layer.\|[0038] In accordance with some embodiments, a shock pad (not shown) may be employed to achieve a desired shock absorption in accordance with a particular installation/purpose. For example, a shock pad (not shown) may be positioned below the one or more infill layers 104 shown in FIG. 1. As such, the material of the infill layers 104 conveys many of the mechanical properties that may be desired for use as artificial turf infill. As shown in the depicted embodiment, the backing 110 may be positioned below the infill layers 104 shown in FIG. 1. In such embodiments, the permeable backing may correspond to the material into which the turf fibers 112 are woven, held, inserted, etc.\|[0039] In an embodiment where the rock dust 102 is incorporated in the synthetic turf system 100 as a top dressing, the rock dust 102 is periodically dispersed over the top portion 114 of the turf fibers 112 with an application system 130 depicted in FIG. 2. With continued reference to FIG. 2, the application system 130 includes a seed tender 132 and a tractor 134 that disperses the rock dust 102 over the synthetic turf system 100 from a broadcaster tool 140. The seed tender 132 is employed in conjunction with a hydraulically-controlled conveyor 142 and a hopper gate 144, which supply the tractor 134 the rock dust 102. As the tractor 134 moves at a consistent speed across the synthetic turf system 100 following a predetermined pattern, the hydraulically-controlled conveyor 142 and the hopper gate 144 precisely control a flow rate of the rock dust 102 to the tractor 134, ensuring uniform distribution across the synthetic turf system 100.\|[0040] While, as depicted, the application system 130 includes the broadcaster tool 140 pulled by the tractor 134, and continuously fed the rock dust 102 by the seed tender 132 along or across the synthetic turf system 100, the application system 130 may additionally or alternatively include a variety of components configured to spread granular material across a field, such as, for example, a self-propelled, manually powered, or power take-off (PTO) driven broadcast material spreader, a pneumatic spreader, an air boom spreader, a drop spreader, a handheld spreader, or an aerial spreader for dispersing the rock dust 102 without departing from the scope of the present disclosure.\|[0041] Once the rock dust 102 is dispersed across the synthetic turf system 100 by the application system 130, the rock dust 102 is brushed into the one or more infill layers 104, including the first layer 120, the second layer 122, and the third layer 124. In this regard, a brush 150 depicted in FIG. 3 grooms the rock dust 102 into the one or more infill layers 104. Rotary brush action on the synthetic turf system 100 from the top portion 114 by the brush 150 effectively works the rock dust 102 downward between the turf fibers 112, ensuring proper placement within the infill material forming the one or more infill layers 104, while maintaining structural integrity and performance characteristics of the synthetic turf system 100, including at the top portion 114 and the first layer 120.\|[0042] While, as depicted, the brush 150 is a motorized, walk-behind rotary brush apparatus, such as a Shindaiwa or Laymor brush system, the brush 150 may additionally or alternatively include various components for incorporating the rock dust 102 into the one or more infill layers 104 such as, for example, a ride-on turf groomer, a tractor-mounted brush that is dragged or PTO driven, or manual turf brushing equipment. Furthermore, brushes employed in such configurations may embody various shapes, sizes, and types, such as, for example, straight brushes, triangular brushes, hydraulic brushes, oscillating brushes, rigid brushes, flexible brushes, or brush assemblies including at least one plurality of brushes. Furthermore, the brush 150 may additionally or alternatively include specialty turf equipment, such as a vacuum or other devices complementary to the brush 150, and utilized to integrate the rock dust 102 into the existing infill material of the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0043] Turning now to FIG. 4, there is shown a more detailed three-dimensional cross-sectional view of a portion of the synthetic turf system 100 utilizing the rock dust 102 as a ballast infill material in accordance with the embodiment set forth above in FIG. 1. It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the rock dust 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-7 are intended solely as one non-limiting example of turf carpet systems in which the rock dust 102 may be utilized.\|[0044] As shown in FIG. 4, the synthetic turf system 100, in addition to including the turf fibers 112, the rock dust 102, the infill layers 104, and the backing 110, further includes a first base stone layer 200 disposed below the backing 110 and above a second base stone layer 202. The synthetic turf system 100 further includes a geotextile component 204 that is a fabric disposed between the second base stone layer 202 and a subgrade 210. The synthetic turf system 100 may further include a subdrain trench component 212 formed in the subgrade and housing a drainage pipe 214.\|[0045] The synthetic turf system 100 may include the rock dust 102 in the infill layers 104, or further include a layer of the rock dust 102 disposed above or below the one or more infill layers 104. In the embodiment of FIG. 4, the rock dust 102 is applied to a top surface of the first base stone layer 200, below the backing 110 and the shock pad. More specifically, the rock dust 102 is layered directly on the top surface of the first base stone layer 200, and forms a continuous layer along the backing 110, where the layer of the rock dust 102 has a thickness of at least one eighth of an inch. Application may be made via a suitable top-dressing machine, as described above. In an embodiment, the rock dust 102 may be deposited with a thickness in the range of about ⅛″ to ¼″. In such an embodiment, rainwater would flow directly through the infill layers 104, the backing 110, and the rock dust 102, and flow into the first base stone layer 200.\|[0046] The rock dust 102 is accessible to rainwater from the top portion 114 of the turf fibers 112, where the rainwater and the rock dust 102 chemically react with each other, forming a carbonate or a bicarbonate. More specifically, in operation, as rainwater contacts the rock dust 102, a chemical reaction occurs between carbonic acid naturally present in the rainwater and the rock dust. The reaction weathers the rock dust 102, e.g., silicate rock, igneous rock, or other reactive rock, rock blends, combinations thereof, etc., and converts the carbonic acid into a carbonate or bicarbonate. In this regard, the rock dust 102 may include wollastonite, basalt, peridotite, dunite, dolomitic lime, dolostone, andesite, diorite, gabbro, rhyolite, olivine, quick lime, lime stone, and other minerals in varying proportions effective for reacting with carbonic acid in rainwater.\|[0047] The weathering rate and shape of particles forming the rock dust 102 are influenced by material selection and particle size distribution. In this regard, consistent particle sizing promotes uniform weathering rates across the one or more infill layers 104, maintaining overall field performance and carbon sequestration efficiency in the synthetic turf system 100. The rock dust 102 is accessible to rainwater traveling downward by gravity from the top portion 114 of the turf fibers 112 toward the backing 110. As the rock dust 102 weathers through exposure to rainwater, its constituent particles may substantially change morphology, or alternatively may remain largely the same shape. In embodiments, the selected silicate rock, igneous rock, or reactive rock materials form weathered particles that maintain a sphericity of about 0.65 to about 0.85. This sphericity range supports stable packing within the synthetic turf system, reduces compaction variability, and ensures continued mechanical performance while facilitating consistent chemical reactions for carbon capture.\|[0048] The rock dust 102 has a particle size distribution that optimizes contact surface area and reactivity with rainwater, without preventing drainage of the rainwater from the synthetic turf system 100. In this regard, a majority of the particles forming the rock dust 102 may be silt, very fine sand, or fine sand in accordance with the Wentworth aggregate classification scheme. In such an embodiment, for example, at least 90 percent of the rock dust 102 by weight may have a particle size greater than 4 micrometers and less than 250 micrometers. In a further embodiment, at least 90 percent of the rock dust 102 by weight may have a particle size less than 125 micrometers. In a further embodiment, at least 90 percent of the rock dust 102 by weight may have a particle size less than 62 micrometers.\|[0049] The infill material forming the infill layers 104 may also include additional materials such as organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust 102. In an embodiment, the rock dust 102 forms less than 10 percent of the infill by weight, as compared to the additional materials. In such an embodiment, the additional materials may be sized and shaped to provide an engineered drainage surface in the synthetic turf system 100, where the rock dust 102 reacts with rainwater without forming an impermeable barrier in the infill layers 104 or otherwise effectively blocking, clogging, or pooling flow of rainwater through the synthetic turf system 100.\|[0050] As stated above, the conversion of the carbon dioxide into other substances, such as carbonate and bicarbonate substances prevents the release of the carbon dioxide into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These carbonate or bicarbonate substances permeate the first base stone layer 200 and the second base stone layer 202, through the geotextile component 204 and into the subdrain trench component 212 and drainage pipe 214. Thereafter, the carbonate or bicarbonate substances are carried by rivers to the sea, where they are ultimately deposited as carbonate sediments such as limestone and dolomites, forming a sink for carbon dioxide.\|[0051] Turning now to FIG. 5, there is shown the synthetic turf system 100 utilizing the rock dust 102 in accordance with another embodiment. In the embodiment depicted in FIG. 5, the rock dust 102 is incorporated into the first base stone layer 200. In accordance with one non-limiting example, the first base stone layer 200 may be implemented as layer of stone having a thickness in the range of about 1 inch to 4 inches, and in some particular embodiments, in the range of about 1 inch to about 2 inches. In such embodiments, the first base stone layer 200 may include ASTM #89 stone or the like. The rock dust 102 may be suitably mixed with the stone to distribute the rock dust 102 throughout the first base stone layer 200. Mixing of the rock dust 102 with the first base stone layer 200 may be accomplished on-site, remotely, e.g., quarry, mine, etc., or the like. As described in greater detail above, reaction of the rock dust 102 with rainwater would occur as described above with respect to FIGS. 1 and 4.\|[0052] Turning now to FIG. 6, there is shown another embodiment of the synthetic turf system 100 utilizing the rock dust 102. As illustrated in FIG. 6, the rock dust 102 is disposed or layered on the geotextile component 204. In such a position, the layer of the rock dust 102 disposed on the geotextile component 204 may have a thickness of ¼″ to ½″. Stated another way, the layer of the rock dust 102 may be applied at the bottom of the second base stone layer 202, as shown in FIG. 6. Application of the layer of the rock dust 102 in FIG. 6 may be accomplished, for example and without limitation, via a suitable top-dressing machine.\|[0053] In accordance with one non-limiting example, the second base stone layer 202 may be implemented as layer of stone having a thickness in the range of about 2 inch to 6 inches, and in some particular embodiments, in the range of about 3 inches to about 4 inches. In such embodiments, the second base stone layer 202 may include ASTM #57 stone or the like. In this manner, the first base stone layer 200 is formed from stone having a first nominal size range, the second base stone layer 202 disposed below the first base stone layer 200 has a second nominal size range coarser than the first nominal size range, and the rock dust 102 is layered above, layered below, or mixed the first base stone layer 200 or the second base stone layer 202. Further, with this construction, the first base stone layer 200 and the second base stone layer 202 are water permeable, and the rock dust 102 is accessible by rainwater traveling from the top portion 114 of the turf fibers 112, through the one or more infill layers 104 by gravity\|[0054] Further, reaction of rock dust 102 with rainwater would occur as described above with respect to FIGS. 1, 4, and 5. It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|[0055] Referring now to FIG. 7, there is shown another embodiment of the synthetic turf system 100 utilizing rock dust 102 for carbon sequestration. As illustrated in FIG. 7, a layer of the rock dust 102 is positioned at a bottom of the subdrain trench component 212. In such an embodiment, the rock dust 102 may be placed at the lowest elevation within the system 100 to maximize the possibility of water coming into contact with the rock dust 102. In some embodiments, although not shown, the rock dust 102 may also be placed below the geotextile component 204, preventing the rock dust 102 from clogging up the drainage system at or between the geotextile component 204 and the subdrain trench component 212, or from being washed down stream. Accordingly, the elevation of the drainage pipe 214 as a storm drain outlet may be utilized to maximize the contact time with the storm water, effectively maximizing the weathering and carbon dioxide capture of the rock dust 102.\|[0056] Although not shown, it is contemplated that the rock dust 102 may be blended with the stone of the second base stone layer 202 similar to the manner described above with respect to FIGS. 1 and 4-6. Similarly, although not illustrated in the accompanying figures, it is further contemplated that the rock dust 102 may be blended with stone in the subdrain trench component 212. The above described positions of the rock dust 102 would also enable the carbon capture reaction described above with respect to FIGS. 1 and 4-6.\|[0057] Referring now to FIG. 8, there is shown the synthetic turf system 100 utilizing rock dust 102 in accordance with another embodiment. As illustrated in FIG. 8, the rock dust 102 may be tilled and incorporated into the subgrade 210 of the synthetic turf system 100, e.g., soil, sediment, etc. In such an implementation, the geotextile component 204 and the 6″ to 8″ combined thickness of the first base stone layer 200 and the second base stone layer 202 may be installed on the modified subgrade 210 having the rock dust 102 distributed therein. It will be appreciated that more rock dust 102 may be used with this embodiment than the embodiments described above, thereby providing additional carbon sequestration capability. Furthermore, it will be appreciated that by placing the rock dust 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air. That is, as organic matter breaks down it creates additional carbon dioxide. Furthermore, the addition of rock dust 102 in the subgrade 210, in addition to carbon sequestration, may also provide firmer and more permeable subgrade, particularly if the subgrade 210 is formed of soft, silty, or sandy soils. Having rock dust 102 in the subgrade 210 where there is potential for more water availability increases the ability for the weathering reaction to occur, e.g., carbon sequestration. In addition, as described above with respect to FIGS. 1 and 4-7, rainwater reaction with the rock dust 102 provides the aforementioned carbon capture benefits.\|[0058] Referring to FIG. 9, a method 300 for preparing a synthetic turf system will be described according to an exemplary embodiment. FIG. 9 will be described with reference to FIGS. 1-8. For simplicity, the method 300 will be described as a sequence of blocks, but the elements of the method 300 can be organized into different architectures, elements, stages, and/or processes.\|[0059] At block 302, the method 300 includes measuring an aspect of the synthetic turf system 100. More specifically, a user may measure a thickness of an infill layer, such as one of the infill layers 104, may measure an acidity of rainwater at the infill layer, and may measure a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer.\|[0060] At block 304, the method 300 includes preblending or layering the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the rock dust 102 over the top portion 114 of the turf fibers 112. In an embodiment, the method 300 includes determining desired compositional ranges of the rock dust 102 based on the measurement or measurements taken at block 302. In this manner, the wear rate and the minimum volume of the one or more infill layers 104 is controlled by adjusting the compositional ranges of components of the rock dust 102. In an embodiment, the rock dust 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0061] At block 310, the method 300 includes dispersing the rock dust 102 over the top portion 114 of the turf fibers 112, where the rock dust 102 includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through the one or more infill layers 104 by gravity. In an embodiment, dispersing the rock dust 102 includes dispersing a predetermined quantity of the rock dust 102 over the top portion 114 of the turf fibers 112 as a top dressing based on the measurement taken at block 302.\|[0062] At block 312, the method 300 includes grooming the rock dust 102 into the one or more infill layers 104 of the synthetic turf system 100, between the turf fibers 112, at the backing 110 of the synthetic turf system 100. In this regard, the brush 150 grooms the rock dust 102 into and through the one or more infill layers 104, where the rock dust 102 contacts and rests on the backing 110.\|[0063] While specific embodiments are shown and described herein, it is contemplated that alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc. without departing from the spirit and/or scope of the innovation as described in detail. These alternative embodiments are to be included within the spirit and scope of the innovation as described and claimed herein.\|[0064] Although the subject matter has been described in language specific to structural features or methodological acts, it is to be understood that the subject matter of the appended claims is not necessarily limited to the specific features or acts described above. Rather, the specific features and acts described above are disclosed as example aspects.\|[0065] Various operations of aspects are provided herein. The order in which one or more or all of the operations are described should not be construed as to imply that these operations are necessarily order dependent. Alternative ordering will be appreciated based on this description. Further, not all operations may necessarily be present in each aspect provided herein.\|[0066] As used in this application, “or” is intended to mean an inclusive “or” rather than an exclusive “or”. Further, an inclusive “or” may include any combination thereof (e.g., A, B, or any combination thereof). In addition, “a” and “an” as used in this application are generally construed to mean “one or more” unless specified otherwise or clear from context to be directed to a singular form. Additionally, at least one of A and B and/or the like generally means A or B or both A and B. Further, to the extent that “includes”, “having”, “has”, “with”, or variants thereof are used in either the detailed description or the claims, such terms are intended to be inclusive in a manner similar to the term “comprising”.\|[0067] Further, unless specified otherwise, “first”, “second”, or the like are not intended to imply a temporal aspect, a spatial aspect, an ordering, etc. Rather, such terms are merely used as identifiers, names, etc. for features, elements, items, etc. For example, a first channel and a second channel generally correspond to channel A and channel B or two different or two identical channels or the same channel. Additionally, “comprising”, “comprises”, “including”, “includes”, or the like generally means comprising or including, but not limited thereto.\|[0068] Further, the term “in” as used to describe an object with respect to a given direction (e.g., an edge extended in a left-right direction) is intended to denote an orientation that is substantially parallel to the specified direction. In contrast, the term “along” as used to describe an object with respect to a given direction (e.g., an edge extended along a vertical direction) is intended to indicate that a feature or element possesses a common vector component in that direction, even if its overall alignment is not strictly parallel.\|[0069] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions and/or alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc., do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.	(US20250333914)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] The application claims priority to and the benefit of U.S. Provisional Patent Application No. 63/638,100, filed on Apr. 24, 2024, entitled “Carbon Capture System and Method for Synthetic Turf Fields”, which we incorporate by reference in its entirety.\|(US20250333914)\|BACKGROUND\|[0002] Synthetic or artificial turf fields are composed of three primary components—from bottom to top: Shock pad, carpet, and infill. These components are generally assembled on top of a base of compacted stone. The shock pad is optional and serves to convey much of the shock absorption performance of the turf field, required for the safety of those playing on the surface in the case of impact with the surface. The carpet serves to mimic the blades of grass and root zone, conveying the softness and traction of the surface as well as many of the ball interaction properties. The infill is generally constituted of at least two layers, the bottom layer of which serves to weight down and stabilize the carpets that it is laid onto, whereas the top layers serve as an additional interface layer to those playing on the field, conveying surface softness, friction, traction, and much of the mechanical properties of the field that are felt directly by the players.\|[0003] When installation of a synthetic turf field occurs, generally speaking, a living, natural turf field is being replaced with an artificial one. In this process, a living organism, e.g., grass, plants, etc., which naturally removes carbon dioxide from the atmosphere is removed. Additionally, the construction associated with a synthetic turf field, as well as the actual manufacturing of the synthetic turf, result in additional carbon entering the atmosphere.\|SUMMARY\|[0004] The following presents a simplified summary to provide a basic understanding of some aspects of the disclosed subject matter. This summary is not an extensive overview. It is not intended to identify key/critical elements or to delineate the scope of the claimed subject matter. Its sole purpose is to present some concepts in a simplified form as a prelude to the more detailed description presented later.\|[0005] There remains a need for environmentally friendly and ultimately carbon-neutral or carbon-offsetting materials that present good mechanical properties and mechanical resistance, while presenting high availability, easy transportation, and low cost.\|[0006] In aspects, a rock dust-based layer may be positioned immediately below the installation of an synthetic turf system, e.g., below a shock pad, on a top substrate material, e.g., a rock layer. In such a position, the rock dust-based layer may have a thickness of ⅛″ to ¼″.\|[0007] In still other aspects, rock dust-based particles may be blended into a 1″ to 2″ topping stone layer positioned immediately below the shock pad.\|[0008] In yet another aspect, a layer of rock dust-based particles may be positioned on a geotextile or subgrade layer. In such a position, the rock dust-based layer may have a thickness of ¼″ to ½″.\|[0009] In another aspect, a rock dust-based material may be positioned at a bottom of a subdrain trench, below a layer of geotextile fabric.\|[0010] In a further aspect, rock dust-based particles may be tilled or blended into native subgrade material. In such a position, the rock dust-based particles may be blended within the subgrade, e.g., soil, as discussed below.\|[0011] In another aspect, a synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes rock dust, or the synthetic turf system further includes a layer of the rock dust disposed above or below the one or more infill layers. The rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.\|[0012] In another aspect, infill for a synthetic turf system includes rock dust. The rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater. At least 90 percent of the rock dust has a particle size less than 250 micrometers. Organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust in one or more infill layers.\|[0013] In another aspect, a method of preparing a synthetic turf system includes dispersing rock dust over a top portion of turf fibers. The rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|[0014] In each of the foregoing aspects, certain carbon sequestration processes can occur as rainwater interacts with the rock dust-based particles, regardless of the position in the synthetic turf system. Further discussion of the processes referenced above are included in the following description.\|[0015] To the accomplishment of the foregoing and related ends, certain illustrative aspects of the claimed subject matter are described herein in connection with the following description and the annexed drawings. These aspects indicate various ways in which the subject matter may be practiced, all of which are intended to be within the scope of the disclosed subject matter. Other advantages and novel features may become apparent from the following detailed description when considered in conjunction with the drawings.\|[0016] These and other systems, methods, objects, features, and advantages of the present disclosure will be apparent to those skilled in the art from the following detailed description of the preferred embodiment and the drawings.\|[0017] All documents mentioned herein are hereby incorporated in their entirety by reference. References to items in the singular should be understood to include items in the plural, and vice versa, unless explicitly stated otherwise or clear from the text. Grammatical conjunctions are intended to express any and all disjunctive and conjunctive combinations of conjoined clauses, sentences, words, and the like, unless otherwise stated or clear from the context.\|(US20250333914)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] FIG. 1 is a partial perspective view of an example synthetic turf system having an infill made of rock dust in accordance with some embodiments of the present disclosure.\|[0019] FIG. 2 is a perspective view of an example application system employed in dispersing the rock dust over the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0020] FIG. 3 is a perspective view of an example brush employed in grooming the rock dust into the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0021] FIG. 4 is a partial perspective view of an example synthetic turf system having rock dust applied to a top surface of a base stone layer in accordance with some embodiments.\|[0022] FIG. 5 is a partial perspective view of an example synthetic turf system having rock dust incorporated into a base stone layer in accordance with some embodiments.\|[0023] FIG. 6 is a partial perspective view of an example synthetic turf system having the rock dust positioned on a geotextile component in accordance with some embodiments.\|[0024] FIG. 7 is a partial perspective view of an example synthetic turf system having rock dust positioned in a subdrain trench in accordance with some embodiments.\|[0025] FIG. 8 is a partial perspective view of an example synthetic turf system having rock dust diffused into a subgrade in accordance with some embodiments.\|[0026] FIG. 9 is an example process flow for preparing a synthetic turf system.\|(US20250333914)\|DETAILED DESCRIPTION\|[0027] Various aspects of the subject disclosure are now described in more detail with reference to the annexed drawings, wherein like numerals generally refer to like or corresponding elements throughout. It should be understood, however, that the drawings and detailed description relating thereto are not intended to limit the claimed subject matter to the particular form disclosed. Instead, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the described and claimed subject matter.\|[0028] The following disclosure provides many different embodiments, or examples, for implementing different features of the provided subject matter. Specific examples of components and arrangements are described below to simplify the present disclosure. These are, of course, merely examples and are not intended to be limiting. For example, the formation of a first feature over or on a second feature in the description that follows may include embodiments in which the first and second features are formed in direct contact, and may also include embodiments in which additional features may be formed between the first and second features, such that the first and second features may not be in direct contact. In addition, the present disclosure may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.\|[0029] Further, spatially relative terms, such as “beneath,” “below,” “lower,” “above,” “upper” and the like, may be used herein for ease of description to describe one element or feature's relationship to another element(s) or feature(s) as illustrated in the figures. The spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. The apparatus may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein may likewise be interpreted accordingly.\|[0030] Numerical values in the specification and claims of this application should be understood to include numerical values which are the same when reduced to the same number of significant figures and numerical values which differ from the stated value by less than the experimental error of conventional measurement technique of the type described in the present application to determine the value. All ranges disclosed herein are inclusive of the recited endpoint.\|[0031] The term “about” can be used to include any numerical value that can vary without changing the basic function of that value. When used with a range, “about” also discloses the range defined by the absolute values of the two endpoints, e.g., “about 2 to about 4” also discloses the range “from 2 to 4.” For example, the term “about” may refer to plus or minus 10% of the indicated number.\|[0032] In accordance with some aspects described herein, there is provided an synthetic turf system that utilizes a material derived from one or more types of rock dust, including, for example and without limitation, basalt rock dust, igneous rock dust (such as andesite, diorite, gabbro, or rhyolite), limestone-derived dust (such as calcium carbonate-based materials), dolomitic lime (CaO/MgO), ultramafic rock dust (such as peridotite or dunite), industrial byproducts containing reactive silicates or carbonates, a blend of various types of rock dust, combinations thereof, or other similar mineral-based particulate materials. In some embodiments, the rock dust may be used as an intervening layer of material between existing layers of the system, mixed within a particular layer, lining a subdrain trench, on or mixed within a substrate, or combinations thereof. It will further be appreciated that as the rock dust is a natural byproduct of the mining industry, there is no additional carbon footprint from mining.\|[0033] In some embodiments contemplated herein, the rock dust material, when in contact with rainwater, causes a chemical reaction to occur between carbonic acid naturally present in the rainwater and the rock dust. The reaction weathers the rock dust and converts the carbonic acid into a carbonate or bicarbonate. By converting the carbon dioxide into other substances, the carbon dioxide can no longer be released into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These carbonate or bicarbonate substances are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments. These carbonate sediments form a sink for carbon dioxide.\|[0034] Turning now to FIG. 1, there is shown a three-dimensional cross-sectional view of a portion of an synthetic turf system 100 utilizing rock dust 102 for carbon sequestration in accordance with an example implementation of the embodiment described above. As shown in FIG. 1, the synthetic turf system 100 includes one or more infill layers 104, a backing 110, and a plurality of turf fibers 112 that emulate grass blades extending substantially perpendicularly upwards relative to the backing 110. As such, the infill layers 104 are positioned above the backing 110, in between the turf fibers 112, and below a top portion 114 of the turf fibers 112.\|[0035] Infill, as shown in FIG. 1, is representative of material that is deposited directly on top of the backing 110 and forms the infill layers 104 around the turf fibers 112. Infill is interspersed between the turf fibers 112, rising out of the backing 110. As depicted, the infill layers 104 have a total depth that covers a portion of the turf fibers 112, leaving at least part of the top portion 114 exposed and extending above the infill layers 104.\|[0036] In accordance with some embodiments, the infill layers 104 assist in supporting the turf fibers 112 in an upright position from the backing 110, and provide traction and shock absorption. As a general matter, various types of infill arrangements are contemplated. In this regard, the one or more infill layers 104 may be a single homogeneous or graded layer, or a plurality of distinct layers. For example, two layer, three layer, or other further layered arrangements of the one or more infill layers 104 are contemplated. For convenience, the present description primarily discusses two and three layer embodiments.\|[0037] In some embodiments, a first layer 120 of infill material may include, for example and without limitation, styrene-butadiene rubber (SBR) particles ethylene propylene diene monomer (EPDM) rubber, other thermoplastics such as polyvinyl chloride (PVC), composite materials can be used that combine thermoplastics, elastomers, reinforcements and/or fillers or other sufficient material, is incorporated. In accordance with some embodiments, a second layer 122 of infill material depicted in FIG. 1 may include a mixture of materials, e.g., material of the first layer 104 and a sand material. In such embodiments, a third layer 124 of infill material may include the aforementioned sand material, which may be implemented as a ballast layer.\|[0038] In accordance with some embodiments, a shock pad (not shown) may be employed to achieve a desired shock absorption in accordance with a particular installation/purpose. For example, a shock pad (not shown) may be positioned below the one or more infill layers 104 shown in FIG. 1. As such, the material of the infill layers 104 conveys many of the mechanical properties that may be desired for use as artificial turf infill. As shown in the depicted embodiment, the backing 110 may be positioned below the infill layers 104 shown in FIG. 1. In such embodiments, the permeable backing may correspond to the material into which the turf fibers 112 are woven, held, inserted, etc.\|[0039] In an embodiment where the rock dust 102 is incorporated in the synthetic turf system 100 as a top dressing, the rock dust 102 is periodically dispersed over the top portion 114 of the turf fibers 112 with an application system 130 depicted in FIG. 2. With continued reference to FIG. 2, the application system 130 includes a seed tender 132 and a tractor 134 that disperses the rock dust 102 over the synthetic turf system 100 from a broadcaster tool 140. The seed tender 132 is employed in conjunction with a hydraulically-controlled conveyor 142 and a hopper gate 144, which supply the tractor 134 the rock dust 102. As the tractor 134 moves at a consistent speed across the synthetic turf system 100 following a predetermined pattern, the hydraulically-controlled conveyor 142 and the hopper gate 144 precisely control a flow rate of the rock dust 102 to the tractor 134, ensuring uniform distribution across the synthetic turf system 100.\|[0040] While, as depicted, the application system 130 includes the broadcaster tool 140 pulled by the tractor 134, and continuously fed the rock dust 102 by the seed tender 132 along or across the synthetic turf system 100, the application system 130 may additionally or alternatively include a variety of components configured to spread granular material across a field, such as, for example, a self-propelled, manually powered, or power take-off (PTO) driven broadcast material spreader, a pneumatic spreader, an air boom spreader, a drop spreader, a handheld spreader, or an aerial spreader for dispersing the rock dust 102 without departing from the scope of the present disclosure.\|[0041] Once the rock dust 102 is dispersed across the synthetic turf system 100 by the application system 130, the rock dust 102 is brushed into the one or more infill layers 104, including the first layer 120, the second layer 122, and the third layer 124. In this regard, a brush 150 depicted in FIG. 3 grooms the rock dust 102 into the one or more infill layers 104. Rotary brush action on the synthetic turf system 100 from the top portion 114 by the brush 150 effectively works the rock dust 102 downward between the turf fibers 112, ensuring proper placement within the infill material forming the one or more infill layers 104, while maintaining structural integrity and performance characteristics of the synthetic turf system 100, including at the top portion 114 and the first layer 120.\|[0042] While, as depicted, the brush 150 is a motorized, walk-behind rotary brush apparatus, such as a Shindaiwa or Laymor brush system, the brush 150 may additionally or alternatively include various components for incorporating the rock dust 102 into the one or more infill layers 104 such as, for example, a ride-on turf groomer, a tractor-mounted brush that is dragged or PTO driven, or manual turf brushing equipment. Furthermore, brushes employed in such configurations may embody various shapes, sizes, and types, such as, for example, straight brushes, triangular brushes, hydraulic brushes, oscillating brushes, rigid brushes, flexible brushes, or brush assemblies including at least one plurality of brushes. Furthermore, the brush 150 may additionally or alternatively include specialty turf equipment, such as a vacuum or other devices complementary to the brush 150, and utilized to integrate the rock dust 102 into the existing infill material of the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0043] Turning now to FIG. 4, there is shown a more detailed three-dimensional cross-sectional view of a portion of the synthetic turf system 100 utilizing the rock dust 102 as a ballast infill material in accordance with the embodiment set forth above in FIG. 1. It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the rock dust 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-7 are intended solely as one non-limiting example of turf carpet systems in which the rock dust 102 may be utilized.\|[0044] As shown in FIG. 4, the synthetic turf system 100, in addition to including the turf fibers 112, the rock dust 102, the infill layers 104, and the backing 110, further includes a first base stone layer 200 disposed below the backing 110 and above a second base stone layer 202. The synthetic turf system 100 further includes a geotextile component 204 that is a fabric disposed between the second base stone layer 202 and a subgrade 210. The synthetic turf system 100 may further include a subdrain trench component 212 formed in the subgrade and housing a drainage pipe 214.\|[0045] The synthetic turf system 100 may include the rock dust 102 in the infill layers 104, or further include a layer of the rock dust 102 disposed above or below the one or more infill layers 104. In the embodiment of FIG. 4, the rock dust 102 is applied to a top surface of the first base stone layer 200, below the backing 110 and the shock pad. More specifically, the rock dust 102 is layered directly on the top surface of the first base stone layer 200, and forms a continuous layer along the backing 110, where the layer of the rock dust 102 has a thickness of at least one eighth of an inch. Application may be made via a suitable top-dressing machine, as described above. In an embodiment, the rock dust 102 may be deposited with a thickness in the range of about ⅛″ to ¼″. In such an embodiment, rainwater would flow directly through the infill layers 104, the backing 110, and the rock dust 102, and flow into the first base stone layer 200.\|[0046] The rock dust 102 is accessible to rainwater from the top portion 114 of the turf fibers 112, where the rainwater and the rock dust 102 chemically react with each other, forming a carbonate or a bicarbonate. More specifically, in operation, as rainwater contacts the rock dust 102, a chemical reaction occurs between carbonic acid naturally present in the rainwater and the rock dust. The reaction weathers the rock dust 102, e.g., silicate rock, igneous rock, or other reactive rock, rock blends, combinations thereof, etc., and converts the carbonic acid into a carbonate or bicarbonate. In this regard, the rock dust 102 may include wollastonite, basalt, peridotite, dunite, dolomitic lime, dolostone, andesite, diorite, gabbro, rhyolite, olivine, quick lime, lime stone, and other minerals in varying proportions effective for reacting with carbonic acid in rainwater.\|[0047] The weathering rate and shape of particles forming the rock dust 102 are influenced by material selection and particle size distribution. In this regard, consistent particle sizing promotes uniform weathering rates across the one or more infill layers 104, maintaining overall field performance and carbon sequestration efficiency in the synthetic turf system 100. The rock dust 102 is accessible to rainwater traveling downward by gravity from the top portion 114 of the turf fibers 112 toward the backing 110. As the rock dust 102 weathers through exposure to rainwater, its constituent particles may substantially change morphology, or alternatively may remain largely the same shape. In embodiments, the selected silicate rock, igneous rock, or reactive rock materials form weathered particles that maintain a sphericity of about 0.65 to about 0.85. This sphericity range supports stable packing within the synthetic turf system, reduces compaction variability, and ensures continued mechanical performance while facilitating consistent chemical reactions for carbon capture.\|[0048] The rock dust 102 has a particle size distribution that optimizes contact surface area and reactivity with rainwater, without preventing drainage of the rainwater from the synthetic turf system 100. In this regard, a majority of the particles forming the rock dust 102 may be silt, very fine sand, or fine sand in accordance with the Wentworth aggregate classification scheme. In such an embodiment, for example, at least 90 percent of the rock dust 102 by weight may have a particle size greater than 4 micrometers and less than 250 micrometers. In a further embodiment, at least 90 percent of the rock dust 102 by weight may have a particle size less than 125 micrometers. In a further embodiment, at least 90 percent of the rock dust 102 by weight may have a particle size less than 62 micrometers.\|[0049] The infill material forming the infill layers 104 may also include additional materials such as organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust 102. In an embodiment, the rock dust 102 forms less than 10 percent of the infill by weight, as compared to the additional materials. In such an embodiment, the additional materials may be sized and shaped to provide an engineered drainage surface in the synthetic turf system 100, where the rock dust 102 reacts with rainwater without forming an impermeable barrier in the infill layers 104 or otherwise effectively blocking, clogging, or pooling flow of rainwater through the synthetic turf system 100.\|[0050] As stated above, the conversion of the carbon dioxide into other substances, such as carbonate and bicarbonate substances prevents the release of the carbon dioxide into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These carbonate or bicarbonate substances permeate the first base stone layer 200 and the second base stone layer 202, through the geotextile component 204 and into the subdrain trench component 212 and drainage pipe 214. Thereafter, the carbonate or bicarbonate substances are carried by rivers to the sea, where they are ultimately deposited as carbonate sediments such as limestone and dolomites, forming a sink for carbon dioxide.\|[0051] Turning now to FIG. 5, there is shown the synthetic turf system 100 utilizing the rock dust 102 in accordance with another embodiment. In the embodiment depicted in FIG. 5, the rock dust 102 is incorporated into the first base stone layer 200. In accordance with one non-limiting example, the first base stone layer 200 may be implemented as layer of stone having a thickness in the range of about 1 inch to 4 inches, and in some particular embodiments, in the range of about 1 inch to about 2 inches. In such embodiments, the first base stone layer 200 may include ASTM #89 stone or the like. The rock dust 102 may be suitably mixed with the stone to distribute the rock dust 102 throughout the first base stone layer 200. Mixing of the rock dust 102 with the first base stone layer 200 may be accomplished on-site, remotely, e.g., quarry, mine, etc., or the like. As described in greater detail above, reaction of the rock dust 102 with rainwater would occur as described above with respect to FIGS. 1 and 4.\|[0052] Turning now to FIG. 6, there is shown another embodiment of the synthetic turf system 100 utilizing the rock dust 102. As illustrated in FIG. 6, the rock dust 102 is disposed or layered on the geotextile component 204. In such a position, the layer of the rock dust 102 disposed on the geotextile component 204 may have a thickness of ¼″ to ½″. Stated another way, the layer of the rock dust 102 may be applied at the bottom of the second base stone layer 202, as shown in FIG. 6. Application of the layer of the rock dust 102 in FIG. 6 may be accomplished, for example and without limitation, via a suitable top-dressing machine.\|[0053] In accordance with one non-limiting example, the second base stone layer 202 may be implemented as layer of stone having a thickness in the range of about 2 inch to 6 inches, and in some particular embodiments, in the range of about 3 inches to about 4 inches. In such embodiments, the second base stone layer 202 may include ASTM #57 stone or the like. In this manner, the first base stone layer 200 is formed from stone having a first nominal size range, the second base stone layer 202 disposed below the first base stone layer 200 has a second nominal size range coarser than the first nominal size range, and the rock dust 102 is layered above, layered below, or mixed the first base stone layer 200 or the second base stone layer 202. Further, with this construction, the first base stone layer 200 and the second base stone layer 202 are water permeable, and the rock dust 102 is accessible by rainwater traveling from the top portion 114 of the turf fibers 112, through the one or more infill layers 104 by gravity\|[0054] Further, reaction of rock dust 102 with rainwater would occur as described above with respect to FIGS. 1, 4, and 5. It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|[0055] Referring now to FIG. 7, there is shown another embodiment of the synthetic turf system 100 utilizing rock dust 102 for carbon sequestration. As illustrated in FIG. 7, a layer of the rock dust 102 is positioned at a bottom of the subdrain trench component 212. In such an embodiment, the rock dust 102 may be placed at the lowest elevation within the system 100 to maximize the possibility of water coming into contact with the rock dust 102. In some embodiments, although not shown, the rock dust 102 may also be placed below the geotextile component 204, preventing the rock dust 102 from clogging up the drainage system at or between the geotextile component 204 and the subdrain trench component 212, or from being washed down stream. Accordingly, the elevation of the drainage pipe 214 as a storm drain outlet may be utilized to maximize the contact time with the storm water, effectively maximizing the weathering and carbon dioxide capture of the rock dust 102.\|[0056] Although not shown, it is contemplated that the rock dust 102 may be blended with the stone of the second base stone layer 202 similar to the manner described above with respect to FIGS. 1 and 4-6. Similarly, although not illustrated in the accompanying figures, it is further contemplated that the rock dust 102 may be blended with stone in the subdrain trench component 212. The above described positions of the rock dust 102 would also enable the carbon capture reaction described above with respect to FIGS. 1 and 4-6.\|[0057] Referring now to FIG. 8, there is shown the synthetic turf system 100 utilizing rock dust 102 in accordance with another embodiment. As illustrated in FIG. 8, the rock dust 102 may be tilled and incorporated into the subgrade 210 of the synthetic turf system 100, e.g., soil, sediment, etc. In such an implementation, the geotextile component 204 and the 6″ to 8″ combined thickness of the first base stone layer 200 and the second base stone layer 202 may be installed on the modified subgrade 210 having the rock dust 102 distributed therein. It will be appreciated that more rock dust 102 may be used with this embodiment than the embodiments described above, thereby providing additional carbon sequestration capability. Furthermore, it will be appreciated that by placing the rock dust 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air. That is, as organic matter breaks down it creates additional carbon dioxide. Furthermore, the addition of rock dust 102 in the subgrade 210, in addition to carbon sequestration, may also provide firmer and more permeable subgrade, particularly if the subgrade 210 is formed of soft, silty, or sandy soils. Having rock dust 102 in the subgrade 210 where there is potential for more water availability increases the ability for the weathering reaction to occur, e.g., carbon sequestration. In addition, as described above with respect to FIGS. 1 and 4-7, rainwater reaction with the rock dust 102 provides the aforementioned carbon capture benefits.\|[0058] Referring to FIG. 9, a method 300 for preparing a synthetic turf system will be described according to an exemplary embodiment. FIG. 9 will be described with reference to FIGS. 1-8. For simplicity, the method 300 will be described as a sequence of blocks, but the elements of the method 300 can be organized into different architectures, elements, stages, and/or processes.\|[0059] At block 302, the method 300 includes measuring an aspect of the synthetic turf system 100. More specifically, a user may measure a thickness of an infill layer, such as one of the infill layers 104, may measure an acidity of rainwater at the infill layer, and may measure a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer.\|[0060] At block 304, the method 300 includes preblending or layering the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the rock dust 102 over the top portion 114 of the turf fibers 112. In an embodiment, the method 300 includes determining desired compositional ranges of the rock dust 102 based on the measurement or measurements taken at block 302. In this manner, the wear rate and the minimum volume of the one or more infill layers 104 is controlled by adjusting the compositional ranges of components of the rock dust 102. In an embodiment, the rock dust 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0061] At block 310, the method 300 includes dispersing the rock dust 102 over the top portion 114 of the turf fibers 112, where the rock dust 102 includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through the one or more infill layers 104 by gravity. In an embodiment, dispersing the rock dust 102 includes dispersing a predetermined quantity of the rock dust 102 over the top portion 114 of the turf fibers 112 as a top dressing based on the measurement taken at block 302.\|[0062] At block 312, the method 300 includes grooming the rock dust 102 into the one or more infill layers 104 of the synthetic turf system 100, between the turf fibers 112, at the backing 110 of the synthetic turf system 100. In this regard, the brush 150 grooms the rock dust 102 into and through the one or more infill layers 104, where the rock dust 102 contacts and rests on the backing 110.\|[0063] While specific embodiments are shown and described herein, it is contemplated that alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc. without departing from the spirit and/or scope of the innovation as described in detail. These alternative embodiments are to be included within the spirit and scope of the innovation as described and claimed herein.\|[0064] Although the subject matter has been described in language specific to structural features or methodological acts, it is to be understood that the subject matter of the appended claims is not necessarily limited to the specific features or acts described above. Rather, the specific features and acts described above are disclosed as example aspects.\|[0065] Various operations of aspects are provided herein. The order in which one or more or all of the operations are described should not be construed as to imply that these operations are necessarily order dependent. Alternative ordering will be appreciated based on this description. Further, not all operations may necessarily be present in each aspect provided herein.\|[0066] As used in this application, “or” is intended to mean an inclusive “or” rather than an exclusive “or”. Further, an inclusive “or” may include any combination thereof (e.g., A, B, or any combination thereof). In addition, “a” and “an” as used in this application are generally construed to mean “one or more” unless specified otherwise or clear from context to be directed to a singular form. Additionally, at least one of A and B and/or the like generally means A or B or both A and B. Further, to the extent that “includes”, “having”, “has”, “with”, or variants thereof are used in either the detailed description or the claims, such terms are intended to be inclusive in a manner similar to the term “comprising”.\|[0067] Further, unless specified otherwise, “first”, “second”, or the like are not intended to imply a temporal aspect, a spatial aspect, an ordering, etc. Rather, such terms are merely used as identifiers, names, etc. for features, elements, items, etc. For example, a first channel and a second channel generally correspond to channel A and channel B or two different or two identical channels or the same channel. Additionally, “comprising”, “comprises”, “including”, “includes”, or the like generally means comprising or including, but not limited thereto.\|[0068] Further, the term “in” as used to describe an object with respect to a given direction (e.g., an edge extended in a left-right direction) is intended to denote an orientation that is substantially parallel to the specified direction. In contrast, the term “along” as used to describe an object with respect to a given direction (e.g., an edge extended along a vertical direction) is intended to indicate that a feature or element possesses a common vector component in that direction, even if its overall alignment is not strictly parallel.\|[0069] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions and/or alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc., do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.	Family Number\|(116414688)\|116414688\|Title\|(US20250333914 A1)\|Carbon capture system and method for synthetic turf fields\|(WO2025222295 A1)\|Carbon capture system and method for synthetic turf fields\|Advantages / Prev. Drawbacks\|(US20250333914 A1)\|Furthermore, it will be appreciated that by placing the rock dust 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air.\|It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|(WO2025222295 A1)\|It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|Independent Claims\|(US20250333914 A1)\| (...) rock dust including silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, wherein at least 90 percent of the rock dust has a particle size less than 250 micrometers in diameter; and\| (...) dispersing rock dust over a top portion of turf fibers, wherein the rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|(WO2025222295 A1)\|14. Infill for a synthetic turf system, the infill comprising: rock dust including silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, wherein at least 90 percent of the rock dust has a particle size less than 250 micrometers in diameter; and organic particles, rubber particles, elastomer (...) \|17. A method of preparing a synthetic turf system, the method comprising: dispersing rock dust over a top portion of turf fibers, wherein the rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|	Civil engineering\|Environmental technology	E01C-013/02\|E01C-013/08		E01C-013/02\|E01C-013/08	B01D-053/62\|E01C-013/02\|E01C-013/08\|E01H-015/00	B01D-053/62\|E01C-013/02\|E01C-013/08\|E01H-015/00					JP2006219870\|US20110081506\|EP3929246	JP2006219870 32443123 WHO=Examiner SELF=N CAT=Y\|US20110081506 7741571 WHO=Examiner SELF=N CAT=X CAT=Y\|EP3929246 97939753 WHO=Examiner SELF=N CAT=A		US20110081506; JP2006219870; EP3929246\|		PENDING	(US20250333914)\|PENDING\|(WO2025/222295)\|PENDING	ALIVE	(US20250333914)\|ALIVE\|(WO2025/222295)\|ALIVE	(US20250333914)\|LEGAL DETAILS FOR US20250333914\|Actual or expected expiration date=2045-04-23\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-04-23\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19186905\|Application date=2025-04-23\|Standardized application number=2025US-19186905\|Event publication date=2025-04-23\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-04-23\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-04-23\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 58213-00341\|Event publication date=2025-04-23\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 136458\|Event publication date=2025-04-23\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2025-04-23\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-04-23\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-04-29\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-05-22\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-05-28\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2025-06-10\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-06-10\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-10-30\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250333914\|Publication stage code=A1\|Publication date=2025-10-30\|Standardized publication number=US20250333914\|Event publication date=2025-10-30\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2025-11-06\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|(WO2025/222295)\|LEGAL DETAILS FOR WO2025/222295\|Actual or expected expiration date=2027-10-24\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-04-23\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOCA2025/050589\|Application date=2025-04-23\|Standardized application number=2025WO-CA50589\|Event publication date=2025-10-30\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/222295\|Publication stage code=A1\|Publication date=2025-10-30\|Standardized publication number=WO2025222295\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2045-04-23\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP25793131\|Event publication date=2025-12-10\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP	(WO2025/222295)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/222295)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/222295)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/222295)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/222295)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UY, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(US20250333914)\|US\|(WO2025/222295)\|WO; EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcPHl2qs/cUhz3ePXCJGwxO7JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023092496&ekey=2099&xpn=US20250333914&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19186905/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=KfuhNexKo8%252FE99EbR8WxkcRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2025/222295)\|CA\|(US20250333914)\|CA	(WO2025/222295)\|NAME=TARKETT SPORTS CANADA INC. 7445 Cote-de-Liesse Road, Suite 200 Montreal, Québec H4T 1G2 , COUNTRY=CA\|(US20250333914)\|NAME=Tarkett Sports Canada Inc. , CITY=Montreal , COUNTRY=CA	(WO2025/222295)\|CA	(WO2025/222295)\|NAME=YIP, Vincent Suite 2400-745 Thurlow Street Vancouver, British Columbia V6E 0C5 , POSTCODE=V6E 0C5 , COUNTRY=CA	(US20250333914)\|CA; CA; US\|(WO2025/222295)\|CA; CA; US	(US20250333914)\|NAME=Smollett Jason, CITY=Kirkland, COUNTRY=CA \|NAME=Habib Eric, CITY=Pierrefonds, COUNTRY=CA \|NAME=Chisam Christopher, CITY=Granite Bay, STATE=CA , COUNTRY=US\|(WO2025/222295)\|NAME=SMOLLETT, Jason 71 Rondeau Kirkland, Québec H9H4J2, POSTCODE=H9H4J2, COUNTRY=CA \|NAME=HABIB, Eric 4967 Saint Barnabas Pierrefonds, Québec H8Z3B9, POSTCODE=H8Z3B9, COUNTRY=CA \|NAME=CHISAM, Christopher 9792 Swan Lake Drive Granite Bay, California 95746, POSTCODE=95746, COUNTRY=US	(WO2025/222295)\|9\|(US20250333914)\|9	2	2					(US20250333914)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,14,17\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|\|(WO2025/222295)\|Number of Claims: NCL=20\|Extended kind: EXTK=x\|	(US20250333914)\|Provisional Appl: US63/638,100 FDD=2024-04-24 [2024US-63638100]	(US20250333914)\|ENGLISH (ENG)	(US20250333914)\|Patent\|(WO2025222295)\|Patent	Titre: (US20250333914)\|Carbon capture system and method for synthetic turf fields Résumé: (US20250333914)\|A synthetic turf system including a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes rock dust, or the synthetic turf system further includes a layer of the rock dust disposed above or below the one or more infill layers. The rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.	18	Abstract	gpt-4o-mini	yes	The article describes a system that uses rock dust in synthetic turf to chemically react with rainwater, forming carbonates or bicarbonates, which aligns with the goal of carbon sequestration.
19	capturing (...) \|(WO2023114474 A2)\|1. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; and capturing CO2 from air using the hydroxide-rich stream (...) \|13. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising salt water and at least one of a mineral and a metal; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; capturing CO2 from (...) \|17. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process comprising electrolysis with an electrolysis unit to produce at least one hydroxide-rich stream; capturing CO2 from air (...) \|(AU2022413289 A1)\|1. A method for capturing and sequestering carbon dioxide (002)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; and capturing 002 from air using the hydroxide-rich stream (...) \|13. A method for capturing and sequestering carbon dioxide (002)	comprising: receiving an input liquid comprising salt water and at least one of a mineral and a metal; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; capturing 002 from (...) \|17. A method for capturing and sequestering carbon dioxide (002)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process comprising electrolysis with an electrolysis unit to produce at least one hydroxide-rich stream; capturing 007 from air (...) \|(CA3241195 A1)\| (...) A method for capturing and sequestering carbon dioxide (002)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; and capturing CO2 from air using the hydroxide-rich stream (...) \|13. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising salt water and at least one of a mineral and a metal; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; capturing CO2 from (...) \|17. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process comprising electrolysis with an electrolysis unit to produce at least one hydroxide-rich stream; capturing CO	from air (...) \|(KR20240134132 A)\|1. A method for capturing and isolating carbon dioxide (CO2)	the method comprising:receiving an input liquid comprising water and a salt;performing an electrochemical process on the input liquid to produce at least one hydroxide rich stream; and capturing CO2 from (...) \|13. A method for capturing and isolating carbon dioxide (CO2)	comprising:receiving an input liquid comprising salt water and at least one of a mineral and a metal;performing an electrochemical process on the input liquid to produce at least one hydroxide rich stream;capturing (...) \|17. A method for capturing and isolating carbon dioxide (CO2)	the method comprising:receiving an input liquid comprising water and a salt;performing an electrochemical process comprising electrolysis with an electrolysis unit to produce at least one hydroxide rich stream;capturing (...) \|(JP2024545883 A)\|1. A method for capturing and isolating carbon dioxide (CO2)	the method comprising the steps of: receiving a feed liquid containing water and a salt; subjecting the feed liquid to an electrochemical process to produce at least one hydroxide-rich stream; and trapping CO2 (...) \|13. A method for capturing and isolating carbon dioxide (CO2)	which comprises the steps of: receiving a feed liquid containing salt water	a mineral and/or a metal; producing at least one hydroxide-rich stream by subjecting the feed liquid to an electrochemical process; capturing (...) \|17. A method for capturing and isolating carbon dioxide (CO2)	which comprises the steps of: receiving a charged liquid containing water and a salt; producing at least one hydroxide-rich stream by conducting an electrochemical process including electrolysis with an electrolysis (...) \|"	Chemical engineering\|Environmental technology\|Materials, metallurgy\|Surface technology, 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1682257 WHO=Applicant SELF=N\|WO200029326 1279369 WHO=Applicant SELF=N\|WO200010691 1466053 WHO=Applicant SELF=N		\|US20210001270; US20100150802; KR20160034635; US20140301922; US20110135551; US20110203939\|US20210001270; US20100150802; KR20160034635; US20140301922; US20110135551; US20110203939; WO201181254; FR2998811; US20120312697; US3712025; WO2020163513; US20080245672; US20200291901\|\|\|\|\|US20210001270; US20110203939; US20100150802; US7637093; US8470275; US8551221; US9422176; US9689309; US9784140; US20060051274; US20100150802; US20110094230; US20110135551; US20110203939; US20110226010; US20140301922; US20180036685; US20200370001; US20210001270; EP2070583; EP3074349; EP3765174; JP3174102U; JP5932771; JP2019194154; KR20140042394; KR20160034635; KR102032948; TWI708740; WO2010104751; WO200010691; WO200029326	\|(US12030016)\|Applicant references\|-Holmes, G. J., “A carbon dioxide absorpiton performance evaluation for capture from ambient air”, 2010, Publisher: University of Calgary, Published in: Calgary.\|-Baciocchi et al., “Process design and energy requirements for the capture of carbon dioxide from air”, 2006.\|-Caldeira et al., “Accelerating carbonate dissolution to sequester carbon dioxide in the ocean: Geochemical implications”, 2000.\|-Dong et al., “Direct Air Capture via Natural Draft Dry Cooling Tower”, 2021.\|-Du et al., “Treatment of Brackish Water RO Brine via Bipolar Membrane Electrodialysis”, 2021.\|-Gmar et al., “Recent advances on electrodialysis for the recovery of lithium from primary and secondary resources”, 2019.\|-Hanein et al., “Decarbonisation of calcium carbonate at atmospheric temperatures and pressures, with simultaneous CO2 capture, through production of sodium carbonate”, Energy & Environmental Science, 2021, p. 65956604, vol. 14, No. 6595.\|-Herrero-Gonzalez et al., “Highly concentrated HCI and NaOH from brines using electrodialysis with bipolar membranes”, 2020.\|-Holmes et al., “Outdoor prototype results for direct atmospheric capture of carbon dioxide”, 2013.\|-House et al., “Economic and energetic analysis of capturing CO2 from ambient air”, 2011.\|-Jiang et al., “Production of Lithium Hydroxide from Lake Brines through ElectroElectrodialysis with Bipolar Membranes (EEDBM)”, 2014.\|-Keith et al., “A Process for Capturing CO2 from the Atmosphere”, 2018, Publisher: Elsevier.\|-Kim, D.H., “A review of desalting process techniques and economic analysis of the recovery of salts from retentates”, 2011.\|-Kuldeep et al., “Bipolar Membrane Electrodialysis for Sulfate Recycling in the Metallurgical Industries”, 2021.\|-Maharloo et al., “Process intensification and environmental consideration of sodium bicarbonate production in an industrial soda ash bubble column reactor by CO2 recycling”, 2017.\|-Mahmoudkhani et al., “Low-energy sodium hydroxide recovery for CO2 capture from atmospheric airThermodynamic analysis”, 2009.\|-Newsom, Gavin, “Selective Recovery of Lithium from Geothermal Brines”, 2020.\|-Pohorecki et al., “Kinetics of Reaction Between Carbon Dioxide and Hydroxyl Ions in Aqueous Electrolyte Solutions”, 1988.\|-Renforth et al., “Assessing ocean alkalinity for carbon sequestration”, 2017.\|-Digdaya et al., “A direct coupled electrochemical system for capture and conversion of CO2 from oceanwater”, Nature Communications, 2020.\|-Du et al., “Supporting Information for Sodium Hydroxide Production from Seawater Desalination Brine: Process Design and Energy efficiency”, Environmental Science & Technology, 2018, Published in: US.\|-Holmes et al., “An air-liquid contactor for large-scale capture of CO2 from air”, Philosophical Transactions of The Royal Society, 2012, pp. 4380-4403, vol. 370.\|-Sanz-Perez et al., “Direct Capture of CO2 from Ambient Air”, Chemical Reviews, 2016, pp. 11840-11876, vol. 116.\|-Smith, Stephen V., “Parsing the Oceanic Calcium Carbonate Cycle: A Net Atmospheric Carbon Dioxide Source, or a Sink?”, 2013.\|-Renforth et al., “Engineering challenges of ocean liming”, 2013.\|-Ruiz et al., “Sustainable and Negative Carbon Footprint Solid-Based NaOH Technology for CO2 Capture”, 2020.\|-Saberi et al., “Precipitation kinetics of sodium bicarbonate in an industrial bubble column crystallizer”, 2009.\|-Sen et al., “Hydroxide Based Integrated CO2 Capture from Air and Conversion to Methanol”, 2020.\|-Shaikh et al., “Scale-up of Bubble Column Reactors: A Review of Current State-of-the-Art”, 2013.\|-Shim et al., “Experimental study on capture of carbon dioxide and production of sodium bicarbonate from sodium hydroxide”, 2016.\|-Socolow et al., “Direct Air Capture of CO2 with Chemicals”, 2011.\|-Song et al., “Separation of sodium hydroxide from post-carbonation brines by bipolar membrane electrodialysis (BMED)”, 2021.\|-Sujoto et al., “Lithium recovery from synthetic geothermal brine using electrodialysis method”, 2021.\|-Telzhensky et al., “Selective separation of seawater Mg2+ ions for use in downstream water treatment processes”, 2011.\|-Wang et al., “Packing characterization for post combustion CO2 capture: mass transfer model development”, 2014.\|-Warren, I., “Techno-Economic Analysis of Lithium Extraction from Geothermal Brines”, 2021.\|-Wylock et al., “Compartmental Modeling of an Industrial Column”, 2009.\|-Xue et al., “Total alkalinity minus dissolved inorganic carbon as a proxy for deciphering ocean acidification mechanisms”, 2020.\|-Zeman et al., “Production of carbon negative precipitated calcium carbonate from waste concreate”, 2016.\|-Du et al., “Sodium hydroxide production from seawater desalination brine: process design and energy efficiency”, 2018.\|-Amaral et al., “Modelling gas-liquid mass transfer in wastewater treatment: when current knowledge needs to encounter engineering practice and vice versa.” Water Science & Technology \| 80.4 \| 2019.\|-Andersen, C. Brannon., “Understanding Carbonate Equilibria by Measuring Alkalinity in Experimental and Natural Systems.” Journal of Geoscience Education, v. 50, n. 4, Sep. 2002, p. 389-403.\|-Ayirala, S.C. and Yousef, A.A., “A Critical Review of Alternative Desalination Technologies for Smart Waterflooding.” Oil and Gas Facilities, Oct. 2016.\|-Ayoub, George M., Ramez M. Zayyat, and Mahmoud Al-Hindi., “Precipitation Softening: A Pretreatment Process for Seawater Desalination.” Environmental Science and Pollution Research 21, No. 4 (Feb. 1, 2014): 2876-87. https://doi.org/10.1007/s11356-013-2237-1.\|-Dahmani et al., “Removal of Ca(II) and Mg(II) hardness by ion exchange resins and soda ash for seawater pretreatment to reduce scale formation in evaporators multi-stage flash desalination.” Desalination and Water Treatment 221 (2021) 23-30.\|-Kiepe et al. “Experimental Determination and Prediction of Gas Solubility Data for CO2 + H2O Mixtures Containing NaCI or KCI at Temperatures between 313 and 393 K and Pressures up to 10 MPa.” Ind. Eng. Chem. Res. 2002, 41, 4393-4398.\|-Kucka et al., “Kinetics of the Gas-Liquid Reaction between Carbon Dioxide and Hydroxide Ions.” Ind. Eng. Chem. Res. 2002, 41, 5952-5957.\|-Macedonio, F., and E. Drioli. “4.09—Membrane Systems for Seawater and Brackish Water Desalination.” In Comprehensive Membrane Science and Engineering, edited by Enrico Drioli and Lidietta Giorno, 241-57. Oxford: Elsevier, 2010. https://doi.org/10.1016/B978-0-08-093250-7.00056-6.\|-Mahmoudkhani et al., “Low energy packed tower and caustic recovery for direct capture of CO2 from air.” Energy Procedia 1 (2009) 1535-1542.\|-“Mazzotti et al., “Direct air capture of CO2 with chemicals: optimization of a two-loop hydroxide carbonate system usinga countercurrent air-liquid contactor.” Climatic Change (2013) 118:119-135”.\|-Nelson et al., “Remineralization and Stabilization of Desalinated Water.”, 2021, https://www.intechopen.com/chapters/78990.\|-Pinsent et al., “The Kinetics of Combination of Carbon Dioxide With Hydroxide Ions.” Dept. of Colloid Science, University of Cambridge, 1956, 1512-1520.\|-Suhalim et al., “A. Rejection Mechanism of lonic Solute Removal by Nanofiltration Membranes: An Overview.”, Nanomaterials Dec. 2022, 437. https://doi.org/10.3390/nano12030437.\|-Thuy et al., “Removal of Hydrogen Sulfide in Synthesized Air by Chemical Absorption in a Packed Column.” Tap chí Khoa hc Công nghe và Thuc pham 18 (2) (2019) 3-11.\|-U.S. Environmental Protection Agency—Office of Water Program Operations, “Physical-Chemical Treatment Technology—Training Manual”, 1977.\|-Voutchkov, Nikolay. “Re-mineralization of Desalinated Water.” 2011.\|\|\|\|\|\|\|	GRANTED	(EP4448148)\|PENDING\|(US12030016)\|GRANTED\|(US20240238721)\|PENDING\|(WO2023/114474)\|LAPSED\|(JP2024545883)\|PENDING\|(KR10-2024-0134132)\|PENDING\|(AU2022413289)\|PENDING\|(CA3241195)\|PENDING	ALIVE	(EP4448148)\|ALIVE\|(US12030016)\|ALIVE\|(US20240238721)\|ALIVE\|(WO2023/114474)\|DEAD\|(JP2024545883)\|ALIVE\|(KR10-2024-0134132)\|ALIVE\|(AU2022413289)\|ALIVE\|(CA3241195)\|ALIVE	(EP4448148)\|LEGAL DETAILS FOR EP4448148\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-12-16\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP22908488\|Application date=2022-12-16\|Standardized application number=2022EP-0908488\|Event publication date=2023-06-24\|Event code=EP/STAAPCT\|Event group=Examination events Entry into national phase\|The international publication has been made\|Original code: STAA\|Event publication date=2024-09-20\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2024-09-20\|Event code=EP/STAARQ\|Event indicator=Pos\|Event group=Examination events\|Request for examination was made\|Original code: STAA\|Event publication date=2024-10-23\|Event code=EP/A2\|Event group=Examination events\|Application published without search report\|Publication country=EP\|Publication number=EP4448148\|Publication stage code=A2\|Publication date=2024-10-23\|Standardized publication number=EP4448148\|Event publication date=2024-10-23\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2024-06-14\|Event publication date=2024-10-23\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC ME MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2025-03-26\|Event code=EP/DAV\|Event indicator=Neg\|Event group=Designated states\|Request for validation of the European patent (deleted)\|Request for validation of the european patent (in any country) deleted\|Event publication date=2025-03-26\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2025-12-10\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2025-12-10\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2025-12-10\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2025-12-10\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2026-04-15\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP4448148\|Publication stage code=A4\|Publication date=2026-04-15\|Standardized publication number=EP4448148\|Event publication date=2026-04-15\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2026-03-18\|Event publication date=2026-04-15\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2026-04-15\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2026-04-15\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2026-04-15\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|(US12030016)\|LEGAL DETAILS FOR US12030016\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2022-12-16\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US18082903\|Application date=2022-12-16\|Standardized application number=2022US-18082903\|Event publication date=2022-12-16\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:PATEL, SMITA S\|Event publication date=2022-12-16\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1732\|Event publication date=2022-12-16\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 9016939/179133\|Event publication date=2022-12-16\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 26386\|Event 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group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-03-20\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2023-03-21\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2023-04-20\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2023-06-13\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2023-06-22\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20230191322\|Publication stage code=A1\|Publication date=2023-06-22\|Standardized publication number=US20230191322\|Event publication date=2023-06-22\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event 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state=ALIVE\|Status=PENDING\|Event publication date=2023-11-14\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US18509020\|Application date=2023-11-14\|Standardized application number=2023US-18509020\|Event publication date=2023-11-14\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:PATEL, SMITA S\|Event publication date=2023-11-14\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1732\|Event publication date=2023-11-14\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 9016939-185891\|Event publication date=2023-11-14\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 26386\|Event publication date=2023-11-14\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business 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Ready for Examination\|Event publication date=2024-04-04\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2024-04-04\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2024-04-05\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2024-04-17\|Event code=US/FLRCPTR\|Event group=Administrative notifications OAO\|Filing Receipt - Replacement\|Event publication date=2024-07-18\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20240238721\|Publication stage code=A1\|Publication date=2024-07-18\|Standardized publication number=US20240238721\|Event publication date=2024-07-18\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2024-09-07\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2026-02-12\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|(WO2023/114474)\|LEGAL DETAILS FOR WO2023/114474\|Actual or expected expiration date=2025-06-16\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-12-16\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2022/053177\|Application date=2022-12-16\|Standardized application number=2022WO-US53177\|Event publication date=2023-06-22\|Event code=WO/A2\|Event group=Examination events\|International application published with declaration under Article 17 (2) (a)\|Publication country=WO\|Publication number=WO2023/114474\|Publication stage code=A2\|Publication date=2023-06-22\|Standardized publication number=WO2023114474\|Event publication date=2023-08-10\|Event code=WO/A3\|Event indicator=Pos\|Event group=Examination events\|Later publication of ISR with revised front page\|Publication country=WO\|Publication number=WO2023/114474\|Publication stage code=A3\|Publication date=2023-08-10\|Standardized publication number=WO2023114474\|Event publication date=2023-11-09\|Event code=WO/DPE1\|Event group=Examination events\|Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)\|Event publication date=2025-06-16\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2022413289\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2022413289\|Application date in the designated or member state=2022-12-16\|Application number in the designated or member state=2022AU-0413289\|Corresponding 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event=2024-07-16\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR JP2024545883\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=JP Corresponding appl: JP2024536084\|Application date in the designated or member state=2022-12-16\|Application number in the designated or member state=2024JP-0536084\|Corresponding cc:\|Designated or member state=JP Corresponding pat: JP2024545883\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2024-12-13\|Publication number in the designated or member state=JP2024545883\|Event publication date=2024-06-14\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=JP\|MEMBER STATE LEGAL DETAILS FOR KR10-2024-0134132\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=KR Corresponding appl: KR10-2024-7023462\|Application date in the designated or member state=2022-12-16\|Application number in the designated or member state=2024KR-7023462\|Corresponding cc:\|Designated or member state=KR Corresponding pat: KR10-2024-0134132\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2024-09-06\|Publication number in the designated or member state=KR20240134132\|Event publication date=2024-07-12\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=KR\|MEMBER STATE LEGAL DETAILS FOR NZ\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=NZ Corresponding appl: NZ808523\|Event publication date=2024-02-22\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=NZ\|(JP2024545883)\|LEGAL DETAILS FOR JP2024545883\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-12-16\|Event code=JP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=JP JP2024536084\|Application date=2022-12-16\|Standardized application number=2024JP-0536084\|Event publication date=2024-12-13\|Event code=JP/A\|Event group=Examination events\|Published application\|Publication country=JP\|Publication number=JP2024545883\|Publication stage code=A\|Publication date=2024-12-13\|Standardized publication number=JP2024545883\|Event publication date=2025-12-12\|Event code=JP/A621\|Event indicator=Pos\|Event group=Examination events\|Written request for application examination\|Japanese intermediate code: A621\|Effective date of the event=2025-12-12\|(KR10-2024-0134132)\|LEGAL DETAILS FOR KR10-2024-0134132\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-12-16\|Event code=KR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=KR KR10-2024-7023462\|Application date=2022-12-16\|Standardized application number=2024KR-7023462\|Event publication date=2024-09-06\|Event code=KR/A\|Event group=Examination events\|Published application\|Publication country=KR\|Publication number=KR10-2024-0134132\|Publication stage code=A\|Publication date=2024-09-06\|Standardized publication number=KR20240134132\|Event publication date=2025-08-27\|Event code=KR/E14\|Event group=Opposition and reexamination events\|PRE-GRANT THIRD PARTY OBSERVATION FILED\|St27 status event code: A-2-3-E10-E14-OPP-X000 (AS PROVIDED BY THE NATIONAL OFFICE)\|(AU2022413289)\|LEGAL DETAILS FOR AU2022413289\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-12-16\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2022413289\|Application date=2022-12-16\|Standardized application number=2022AU-0413289\|Event publication date=2024-03-07\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2022413289\|Publication stage code=A1\|Publication date=2024-03-07\|Standardized publication number=AU2022413289\|(CA3241195)\|LEGAL DETAILS FOR CA3241195\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-12-16\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA3241195\|Application date=2022-12-16\|Standardized application number=2022CA-3241195\|Event publication date=2023-06-22\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA3241195\|Publication stage code=A1\|Publication date=2023-06-22\|Standardized publication number=CA3241195	(EP4448148)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2023/114474)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2023/114474)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2023/114474)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2023/114474)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2023/114474)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, 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NZ\|(JP2024545883)\|JP\|(KR10-2024-0134132)\|KR\|(AU2022413289)\|AU\|(CA3241195)\|CA	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=ECLncZT9nTVX7AnVeY5F63mXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022061326&ekey=2149&xpn=EP4448148&kind=A4	https://register.epo.org/application?number=EP22908488	https://permalink.orbit.com/RenderStaticFirstPage?XPN=atIwPveYDDMbWDK85JFymXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(US20240238721)\|US\|(WO2023/114474)\|US\|(WO2023/114474)\|US\|(US12030016)\|US\|(US20230191322)\|US	(US20240238721)\|NAME=Capture6 Corp. , CITY=Berkeley , STATE=CA , COUNTRY=US\|(WO2023/114474)\|NAME=CAPTURE6 CORP 1340 Josephine St Berkeley, California 94703 , COUNTRY=US\|(WO2023/114474)\|NAME=CAPTURE6 CORP 1340 Josephine St Berkeley, California 94703 , COUNTRY=US\|(US12030016)\|NAME=Capture6 Corp , CITY=Berkeley , STATE=CA , COUNTRY=US , ATYP=US Company\|(US20230191322)\|NAME=Capture6 Corp , CITY=Berkeley , STATE=CA , COUNTRY=US	(EP4448148)\|GB\|\|(WO2023/114474)\|US\|(WO2023/114474)\|US\|\|\|(AU2022413289)\|NZ\|(CA3241195)\|CA	(EP4448148)\|NAME=Dentons UK and Middle East LLP One Fleet Place , CITY=London EC4M 7WS , COUNTRY=GB , REG=101672946\|(US12030016)\|NAME=DENTONS DAVIS BROWN NAME=Warner-Blankenship Matthew\|(WO2023/114474)\|NAME=WARNER-BLANKENSHIP, Matthew 215 10th Street Suite 1300 Des Moines, Iowa 50309 , POSTCODE=50309 , COUNTRY=US\|(WO2023/114474)\|NAME=WARNER-BLANKENSHIP, Matthew 215 10th Street Suite 1300 Des Moines, Iowa 50309 , POSTCODE=50309 , COUNTRY=US\|(JP2024545883)\|NAME=YAMAMOTO Osamu , REG=100118902NAME=MIYAMAE,Toru , REG=100106208NAME=MATSUO JUNICHI , REG=100196508NAME=YOKOTA KOICHI , REG=100196597\|(KR10-2024-0134132)\|NAME=KIM, TAE HONG NAME=KIM, JIN HOI\|(AU2022413289)\|NAME=Dentons Patent Attorneys Australasia Limited 18 Viaduct Harbour Avenue , CITY=Auckland CBD , POSTCODE=1142 , COUNTRY=NZ\|(CA3241195)\|NAME=BORDEN LADNER GERVAIS LLP , COUNTRY=CA	\|(EP4448148)\|US; NZ; US; US\|(US12030016)\|US; US; NZ; US\|(US20230191322)\|NZ; US; US; US\|(US20240238721)\|US; NZ; US; US\|(WO2023/114474)\|US; NZ; US; US\|(WO2023/114474)\|US; NZ; US; US\|\|\|\|(CA3241195)\|US; NZ; US; US	(EP4448148)\|NAME=COHEN-COLE, Ethan\|NAME=SHORS, Luke\|NAME=SURANA, Rahul\|NAME=LANDAU, Zeph\|(EP4448148)\|NAME=COHEN-COLE, Ethan, CITY=Berkeley, California 94703, COUNTRY=US \|NAME=SHORS, Luke, CITY=Rotorua,, COUNTRY=NZ \|NAME=SURANA, Rahul, CITY=Fremont, CA 94539, COUNTRY=US \|NAME=LANDAU, Zeph, CITY=Berkeley, California 94702, COUNTRY=US\|(US12030016)\|NAME=Cohen-Cole Ethan, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Surana Rahul, CITY=Fremont, STATE=CA , COUNTRY=US \|NAME=Shors Luke, CITY=Rotorua, COUNTRY=NZ \|NAME=Landau Zeph, CITY=Berkeley, STATE=CA , COUNTRY=US\|(US20230191322)\|NAME=Shors Luke, CITY=Rotorua, COUNTRY=NZ \|NAME=Landau Zeph, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Cohen-Cole Ethan, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Surana Rahul, CITY=Fremont, STATE=CA , COUNTRY=US\|(US20240238721)\|NAME=COHEN-COLE ETHAN, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Shors Luke, CITY=Rotorua, COUNTRY=NZ \|NAME=Surana Rahul, CITY=Fremont, STATE=CA , COUNTRY=US \|NAME=Landau Zeph, CITY=Berkeley, STATE=CA , COUNTRY=US\|(WO2023/114474)\|NAME=COHEN-COLE, Ethan 1340 Josephine St Berkeley, California 94703, POSTCODE=94703, COUNTRY=US \|NAME=SHORS, Luke 128 Iles Rd Rotorua, COUNTRY=NZ \|NAME=SURANA, Rahul 47066 Palo Amarillo Dr. Fremont, CA 94539, POSTCODE=94539, COUNTRY=US \|NAME=LANDAU, Zeph 1346 Curtis Street Berkeley, California 94702, POSTCODE=94702, COUNTRY=US\|(WO2023/114474)\|NAME=COHEN-COLE, Ethan 1340 Josephine St Berkeley, California 94703, POSTCODE=94703, COUNTRY=US \|NAME=SHORS, Luke 128 Iles Rd Rotorua, COUNTRY=NZ \|NAME=SURANA, Rahul 47066 Palo Amarillo Dr. Fremont, CA 94539, POSTCODE=94539, COUNTRY=US \|NAME=LANDAU, Zeph 1346 Curtis Street Berkeley, California 94702, POSTCODE=94702, COUNTRY=US\|(JP2024545883)\|NAME=Cohen Cole, Ethan\|NAME=Shores, Luke\|NAME=Surana, Rahul\|NAME=Zeff Landau\|(KR10-2024-0134132)\|NAME=COHEN COLE ETHAN\|NAME=SHORS LUKE\|NAME=SURANA RAHUL\|NAME=LANDAU ZEPH\|(AU2022413289)\|NAME=COHEN-COLE, Ethan\|NAME=SHORS, Luke\|NAME=SURANA, Rahul\|NAME=LANDAU, Zeph\|(CA3241195)\|NAME=COHEN-COLE, ETHAN, COUNTRY=US \|NAME=SHORS, LUKE, COUNTRY=NZ \|NAME=SURANA, RAHUL, COUNTRY=US \|NAME=LANDAU, ZEPH, COUNTRY=US	(US20240238721)\|50\|\|(JP2024545883)\|10\|(KR10-2024-0134132)\|50\|(AU2022413289)\|47\|(CA3241195)\|50\|(US12030016)\|50	8	8				(EP4448148)\|WO2023/114474\|(JP2024545883)\|WO2023/114474\|(KR10-2024-0134132)\|WO2023/114474\|(AU2022413289)\|WO2023/114474\|(CA3241195)\|WO2023/114474		(US12030016)\|Number of Claims: NCL=7\|Number of Drawings: NDR=50\|Number of Figures: NFG=50\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=0\|Primary examiner: Patel Smita S\|Art Unit.: ART =1732\|\|(US20230191322)\|Number of Claims: NCL=20\|Number of Drawings: NDR=50\|Number of Figures: NFG=50\|Independent Claim Number: ICL=1,13,17\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|Primary examiner: Patel Smita S\|Art Unit.: ART =1732\|\|(US20240238721)\|Number of Claims: NCL=20\|Number of Drawings: NDR=50\|Number of Figures: NFG=50\|Exemplary Claim Number: ECL=21\|\|(WO2023/114474)\|Number of Claims: NCL=20\|Extended kind: EXTK=z\|\|(JP2024545883)\|Number of Claims: NCL=20\|Request for examination: REQEXA=false\|\|(KR10-2024-0134132)\|Number of Claims: NCL=20\|\|(AU2022413289)\|Number of Claims: NCL=20\|\|(CA3241195)\|Number of Claims: NCL=20\|	(US12030016)\|Provisional Appl: US63/290,467 FDD=2021-12-16 [2021US-63290467]\|Provisional Appl: US63/341,883 FDD=2022-05-13 [2022US-63341883]\|Provisional Appl: US63/355,368 FDD=2022-06-24 [2022US-63355368]\|Provisional Appl: US63/389,095 FDD=2022-07-14 [2022US-63389095]\|Provisional Appl: US63/413,021 FDD=2022-10-04 [2022US-63413021]\|Previous publication: US20230191322 A1 2023-06-22 [US20230191322]\|(US20240238721)\|Continuation of: US18/082,903 FDD=2022-12-16 [2022US-18082903]\|Provisional Appl: US63/413,021 FDD=2022-10-04 [2022US-63413021]\|Provisional Appl: US63/389,095 FDD=2022-07-14 [2022US-63389095]\|Provisional Appl: US63/355,368 FDD=2022-06-24 [2022US-63355368]\|Provisional Appl: US63/341,883 FDD=2022-05-13 [2022US-63341883]\|Provisional Appl: US63/290,467 FDD=2021-12-16 [2021US-63290467]	(EP4448148)\|ENGLISH (ENG)	CC=KR ORG=QUESTEL			(EP4448148)\|Patent\|(JP2024545883)\|Patent\|(EP4448148)\|Patent\|(KR20240134132)\|Patent\|(US20240238721)\|Patent\|(US12030016)\|Patent\|(AU2022413289)\|Patent\|(WO2023114474)\|Patent\|(CA3241195)\|Patent\|(US20230191322)\|Patent\|(WO2023114474)\|Patent				Titre: from air (...) \|(KR20240134132 A)\|1. A method for capturing and isolating carbon dioxide (CO2) Résumé: the method comprising:receiving an input liquid comprising water and a salt;performing an electrochemical process on the input liquid to produce at least one hydroxide rich stream; and capturing CO2 from (...) \|13. A method for capturing and isolating carbon dioxide (CO2)	17	Abstract	gpt-4o-mini	no	The article focuses on capturing and isolating CO2 through an electrochemical process, which does not involve the accelerated weathering of minerals or the specific methods related to enhanced weathering.
20	CN202511559558	CN202511559558	CN121253236	117274553	CN121253236 A 2026-01-02 [CN121253236]	2025-10-29	2025-10-29	2026-01-02		(CN121253236)\|2045-10-29	(CN121253236)\|Buried soil water collecting system	(CN121253236)\|The invention provides a buried soil water collection system, and belongs to the technical field of rock weathering carbon sequestration and salinized soil transformation and governance, a porous ceramic tube is buried in soil, a porous water absorption material and an extrusion assembly for extruding the porous water absorption material are arranged in the porous ceramic tube, and soil water adsorbed in the soil is absorbed by the porous ceramic tube under the capillary action, so that the soil water is absorbed by the porous ceramic tube; the soil water is adsorbed and transmitted to the porous water absorption material through the microporous structure of the porous ceramic tube, and the porous water absorption material can continuously adsorb and store the soil water. When the water storage amount in the porous water absorption material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorption material, so that the soil water stored in the porous water absorption material is extruded out, and the extruded soil water is drained to the water storage container through the water outlet holes in the porous ceramic pipe and the liquid guide pipe, so that the soil water is centrally stored in the water storage container. Therefore, the real soil water sample can be stably and efficiently collected for a long time under the field condition that the in-situ structure and the moisture dynamic state of the soil are not damaged.	LANZHOU UNIVERSITY\|MICROCARBON LOW CARBON TECHNOLOGY	(CN121253236)\|LANZHOU UNIVERSITY ([CN])\|Microcarbon (Guangzhou) Low Carbon Technology Co., Ltd.	ZHANG JIETANG\|LI XINGYUAN\|GOU XIAOHUA	(CN121253236)\|ZHANG JIETANG\|LI XINGYUAN\|GOU XIAOHUA	(CN121253236)\|HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP)\|Reg. Nb: 41028	(CN121253236)\|Compared with the prior art, the buried soil water collecting system provided by the embodiment of the invention has the advantages that the porous ceramic tube 21 with the wall having the micropore structure is buried in soil, the porous water absorbing material 22 capable of absorbing and storing soil water and the extrusion component 3 capable of extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22 are arranged in the porous ceramic tube 21, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic tube 21 under the capillary action, and is absorbed and transmitted to the porous water absorbing material 22 through the micropore structure of the porous ceramic tube 21, so that the porous water absorbing material 22 can continuously absorb and store the soil water.\|It will be appreciated that in some embodiments, the filter layer comprises at least one layer of non-woven fabric, because the non-woven fabric has the advantages of being flexible, light in weight, non-toxic, easy to decompose, low in cost, and the like, the porous ceramic tube 21 can be effectively wrapped by the non-woven fabric as the filter layer, so that the pollution to soil water is avoided, the pollution to soil is low, and meanwhile, the cost of the buried soil water collecting system can be effectively controlled.\|Therefore, in the research and product development of enhancing silicate mineral weathering for improvement of salty soil and carbon fixation, there is a need for a technical scheme capable of efficiently collecting real soil water samples under the condition of not damaging the in-situ structure and the moisture dynamics of soil so as to obtain reliable weathering reaction, salt replacement and carbon fixation process data and promote the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|2) The salt migration data is inaccurate, namely, the surface water sample is often influenced by evaporation, precipitation and surface pollution, and the real migration state of the salt with different depths of the section is difficult to reflect;\|Based on the above problems existing in the prior art, an object of the embodiments of the present invention is to provide a buried soil water collection system capable of efficiently collecting real soil water samples under the condition that the in-situ structure and the moisture dynamics of the soil are not damaged, so as to solve the technical problems in the prior art that soil water samples of different soil layers cannot be collected stably and in situ for a long time under the field condition, and chemical composition and hydraulic characteristics of the collected liquid are difficult to be ensured to be consistent with the soil environment.\|	(CN121253236)\|1. A buried soil water collection system, comprising: A fixed bracket; The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.\|	(CN121253236)\|The invention provides a buried soil water collecting system, which belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction and treatment, wherein a porous ceramic tube is buried in soil, a porous water absorbing material and an extrusion component for extruding the porous water absorbing material are arranged in the porous ceramic tube, under the capillary action, the soil water adsorbed in the soil is adsorbed and transferred to the porous water absorbing material through the micropore structure of the porous ceramic tube, and the porous water absorbing material can continuously adsorb and store the soil water.\|The invention provides a buried soil water collecting system, which can collect soil water samples of different soil layers for a long time, stably and in situ under field conditions, and ensure that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for the mechanism research, the effect evaluation and the product optimization of the multifunctional silicate mineral conditioner in the application of improving and fixing the carbon of the saline soil.\|	(CN121253236)\|POROUS CERAMIC TUBE(100,106)\|SOIL WATER COLLECTION(100,35)\|BURIED SOIL WATER COLLECTION(100,9)\|SOIL MOISTURE DYNAMICS(62,2)\|SALINE SOIL RECONSTRUCTION(60,1)\|NONWOVEN FABRIC(55,6)\|EXPERIMENTAL SIMULATION AUTHENTICITY(52,1)\|BURIED SOIL WATER COLLECTING(51,19)\|MOISTURE DYNAMICS(44,2)\|POROUS WATER(40,47)\|ENHANCING SILICATE MINERAL WEATHERING(39,1)\|RESEARCH SCIENTIFICITY(37,1)\|MULTIFUNCTIONAL SILICATE MINERAL CONDITIONER(33,4)\|EXTRUDING POROUS WATER(32,4)\|SALINE SOIL CARBON(31,1)\|SIMULATION EXPERIMENT(31,1)\|DRIVING ROD(30,31)\|BURYING SOIL(30,2)\|GROUND(29,28)\|EXTRUSION COMPONENT(29,11)\|SOIL SALINITY(29,1)\|PULL ROPE(28,6)\|RELIABLE WEATHERING REACTION(28,1)\|REAL MIGRATION(27,1)\|SOIL ENVIRONMENT(26,4)\|EXTRUDE POROUS WATER(24,7)\|CONTAMINATION(24,2)\|MICROPORE(23,5)\|LIQUID COLLECTION(22,8)\|SOIL WATER(21,76)\|MICROPORE STRUCTURE(21,6)\|GROUND LAYER(21,4)\|MINERAL CONDITIONING AGENT DEVELOPMENT(21,1)\|SILICATE MINERAL CONDITIONER(20,4)\|DRIVING EXTRUSION(20,3)\|MINERAL CONDITIONING AGENT(20,1)\|SLIDING HOLE(19,24)\|PUSH PULL ROD(19,22)\|DYNAMIC MOISTURE(19,1)\|FILTER LAYER(18,15)\|SALT MIGRATION DATA(18,1)\|REAL SOIL WATER SAMPLE(17,5)\|TUBE SECTION(16,24)\|MICROPOROUS STRUCTURE(16,10)\|TUBE WALL(16,6)\|BLOCK SEDIMENT(16,2)\|CAPILLARY ACTION(15,11)\|SOIL WATER ADSORBING MEMBER(15,3)\|OUTLET HOLE(15,2)\|PRECIPITATION(15,1)\|SALTY SOIL(15,1)\|COLUMNAR SPONGE END(14,11)\|CARBON FIXATION(14,9)\|SOIL WATER SAMPLE(14,5)\|SLIDING MEMBER(14,2)\|WATER OUTLET(13,15)\|FIXED BRACKET(13,13)\|SOIL WATER ADSORPTION COMPONENT(13,10)\|POROUS WATER COMPRESSION RATIO(12,5)\|COLUMNAR SPONGE DIRECTION(12,3)\|MECHANISM RESEARCH(12,3)\|POROUS WATER ABSORPTION(12,2)\|CERAMIC TUBE(12,1)\|EFFECT EVALUATION(12,1)\|PUSH PULL TUBE GLASS CERAMIC(12,1)\|PRESSING PIECE(11,16)\|ROCK(11,2)\|SLIDING ROD DRIVING(11,2)\|WATER STORAGE CONTAINER(10,16)\|ELASTIC MEMBER(10,7)\|PRESSING MEMBER DRIVING(10,1)\|WATERTIGHT COMPACT STRUCTURE(10,1)\|SOIL WATER EXTRUSION(9,5)\|ACCURATE EXPERIMENTAL DATA(9,3)\|SYMMETRICAL AXIS(9,3)\|CONNECTING ROD(8,16)\|PISTON ROD(8,10)\|COIL SPRING(8,9)\|POROUS STRUCTURE(8,9)\|REPEATABLE EXPERIMENTAL DATA SUPPORT(8,3)\|SURFACE CONTAMINATION(8,1)\|FIXED SUPPORT(7,8)\|LIQUID GUIDE TUBE(7,8)\|COMPRESSION RATIO(7,7)\|POROUS WATER POROUS STRUCTURE(7,6)\|CHEMICAL COMPOSITION(7,4)\|POROUS WATER ABSORPTION MATERIAL(7,4)\|POROUS CERAMIC PIPE(7,3)\|OUTER PERIPHERAL(6,6)\|SLIDING GROOVE(6,6)\|PISTON OUTER CIRCUMFERENTIAL SURFACE(6,3)\|PRODUCT OPTIMIZATION(6,3)\|EXTRUSION SUBASSEMBLY(6,2)\|MINERAL DISSOLUTION REALITY(6,1)\|PRODUCT DEVELOPMENT(6,1)\|SALINE SOIL RECLAMATION(6,1)\|PIPE SECTION(5,17)\|PULLEY BLOCK(5,8)\|WATER ABSORPTION MATERIAL(5,4)\|COLUMN SPONGE(5,3)\|PULLEY BRACKET(5,2)\|CARBON FIXATION PROCESS DATA(5,1)\|CHINESE SALINE ALKALI SOIL(5,1)\|NONWOVEN FABRICS(5,1)\|POTASSIUM MICROELEMENT(5,1)\|PROCESS DATA(5,1)\|SALINE ALKALI BARREN LAND(5,1)\|WATER STORAGE(4,22)\|OPEN END(4,10)\|FIELD CONDITION(4,4)\|MOISTURE DYNAMIC(4,2)\|SALINIZED SOIL IMPROVEMENT(4,2)\|UNCOMPRESSED(4,2)\|AIRTIGHT COMPACT(4,1)\|ECOLOGICAL SAFETY(4,1)\|ERODE ELASTIC PIECE(4,1)\|EXTENSIVE UTILIZATION(4,1)\|WATERPROOF SEALING(4,1)\|WEATHERING EXPERIMENT(4,1)\|OUTER SIDE(3,7)\|PIPE WALL(3,6)\|MOVEABLE PULLEY(3,5)\|CYLINDRICAL SPRING(3,2)\|ELASTICITY(3,2)\|INNER SIDEWALL(3,2)\|SEALING PERFORMANCE ENHANCEMENT(3,2)\|SLIDING SHAFT(3,2)\|SLIDING SLOT(3,2)\|AIRTIGHT SEALING FILM(3,1)\|ATMOSPHERIC CO2 FIXATION(3,1)\|BLOCKING SEDIMENT(3,1)\|ELASTIC BUFFERING ACTION(3,1)\|ENHANCING SILICATE MINERAL(3,1)\|FINISH EXTRUSION(3,1)\|SALT MIGRATION(3,1)\|CENTRAL POSITION(2,4)\|SPIRAL SPRING(2,4)\|GROUND SECTION(2,3)\|ABSORBENT COTTON(2,1)\|ALKALI ION(2,1)\|ARTIFICIALLY PREPARED LEACHING SOLUTION(2,1)\|BICARBONATE(2,1)\|COLUMNAR SPONGE COMPRESSION RATIO(2,1)\|COLUMNAR SPONGE FLOW(2,1)\|DRENCHING SOLUTION(2,1)\|EVALUATION ERROR(2,1)\|EXCHANGE REACTION NA(2,1)\|EXTENSIVE TREATMENT(2,1)\|ION MIGRATION(2,1)\|KEY INDEX(2,1)\|MICROENVIRONMENT(2,1)\|OPENING END(2,1)\|PIPE CAVITY(2,1)\|SALINE ALKALI LAND(2,1)\|STABLE PROMOTION(2,1)\|SURFACE WATER SAMPLE(2,1)\|	(CN121253236)\|1. A buried soil water collection system, comprising:\| A fixed bracket; \| The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; \| the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; \| The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; \| a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and \|The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.\|2. The buried soil water collecting system according to claim 1, wherein the porous water absorbing material is a columnar sponge, an axial direction of the columnar sponge is parallel to an axial direction of the porous ceramic tube, and an outer peripheral surface of the columnar sponge is in contact with an inner side wall of the porous ceramic tube.\|3. The buried soil water collection system according to claim 2, wherein the extrusion assembly comprises a first pressing member slidably disposed in the porous ceramic tube, a second pressing member slidably disposed in the porous ceramic tube, an elastic member for elastically pressing the second pressing member against the first pressing member, and a push-pull rod for driving the first pressing member to slide against the second pressing member, the first pressing member is disposed adjacent to the closed end of the porous ceramic tube, the first pressing member is abutted against the first end of the columnar sponge, the second pressing member is disposed adjacent to the open end of the porous ceramic tube, the first pressing member is abutted against the second end of the columnar sponge, a first sliding hole for the push-pull rod to pass through is disposed on the second pressing member, a second sliding hole for the rod to pass through is disposed on the columnar sponge, the first end of the push-pull rod extends into the porous ceramic tube via the open end of the push-pull ceramic tube, and the first end of the push-pull rod is sequentially connected to the first sliding member after passing through the first sliding hole and the second sliding member.\|4. The buried soil water collecting system according to claim 3, wherein the elastic member is a coil spring accommodated in the porous ceramic tube, an opening end of the porous ceramic tube is provided with a holding cover for holding the coil spring, one end of the coil spring is held against and fixed on the holding cover, the other end of the coil spring is held against the second holding member, and a third sliding hole for the push-pull rod to pass through is formed in the holding cover.\|5. The system of claim 3, wherein the first pressing member comprises a first piston slidably disposed in the porous ceramic tube and a first pressing member connected to the first piston, wherein an outer circumferential surface of the first piston is in interference contact with an inner side wall of the porous ceramic tube, the first pressing member is in interference contact with a first end of the columnar sponge, and wherein the second pressing member comprises a second pressing member slidably disposed in the porous ceramic tube and connected to the second piston, wherein an outer circumferential surface of the second piston is in interference contact with an inner side wall of the porous ceramic tube, and wherein the second pressing member is in interference contact with a second end of the columnar sponge.\|6. The buried soil water collecting system according to claim 5, wherein the porous ceramic tube comprises a first tube section and a second tube section which are integrally formed, wherein one end of the first tube section away from the second tube section is a closed end, one end of the second tube section away from the first tube section is an open end, a microporous structure capable of adsorbing and transmitting soil water is arranged on a tube wall of the first tube section, the first piston and the columnar sponge are positioned in the first tube section, the tube wall of the second tube section is of a gas-tight and water-tight compact structure, the second piston and the elastic element are positioned in the second tube section, and the water outlet is arranged on the tube wall of the second tube section.\|7. A buried soil water collecting system according to claim 3, wherein a plurality of said soil water adsorbing members are provided in a plurality, said plurality of said soil water adsorbing members being arranged side by side and at intervals, each of said soil water adsorbing members being provided with one said pressing member, each of said pressing members being connected to said driving means.\|8. The buried soil water collecting system according to claim 7, wherein the driving device comprises a sliding rod, a driving rod and a cylinder, wherein the two ends of the sliding rod are respectively arranged on the fixed support in a sliding manner, the driving rod is used for driving the sliding rod to move along the axial direction of the sliding rod, the cylinder is used for driving the driving rod to move along the axial direction of the sliding rod, the axial direction of the sliding rod is perpendicular to the axial direction of the sliding rod, the second end of the sliding rod is connected with the sliding rod, the axial direction of the driving rod is parallel to the axial direction of the sliding rod, the first end of the driving rod is connected with the central position of the sliding rod, and the second end of the driving rod is connected with a piston rod of the cylinder.\|9. The buried soil water collecting system according to claim 8, wherein the number of the cylinders is two, piston rods of the two cylinders are symmetrically distributed by taking a central axis of the driving rod as a symmetrical axis, the driving device further comprises a connecting rod axially perpendicular to the axial direction of the driving rod and two pulley blocks symmetrically arranged on two sides of the driving rod, a pull rope is wound on each pulley block, the axial direction of a vertical section of each pull rope is parallel to the axial direction of the driving rod, one pull rope connects a first end of the sliding rod with a first end of the connecting rod, the other pull rope connects a second end of the sliding rod with a second end of the connecting rod, two ends of the connecting rod are respectively connected with the corresponding piston rods, and the second end of the driving rod is connected with a central position of the connecting rod.\|10. A buried soil water collecting system according to any one of claims 1 to 9 wherein said filter layer comprises at least one layer of non-woven fabric or silt filter screen.	(CN121253236)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reclamation and treatment, and particularly relates to a buried soil water collection system.\|BACKGROUND ART\|[0002] China is a large country of saline-alkali soil, and the third country is the first 10 countries in the area of saline-alkali soil. The Chinese saline-alkali soil is distributed in 17 provinces including northwest, northeast, north China and coastal areas, the total area of the saline-alkali barren lands and the saline-alkali lands affecting the cultivated lands exceeds 5 hundred million mu, and the agricultural production and the ecological safety are seriously restricted. In order to respond to the requirements of comprehensive treatment and comprehensive utilization of saline-alkali soil with stable promotion, development of a multifunctional silicate mineral conditioner with functions of improving saline-alkali soil, supplementing trace elements and fixing carbon is needed. The conditioner relies on the technology of enhancing silicate mineral weathering, and releases Ca 2+、Mg2+ and other exchange reactions Na +、CO2- 3、HCO-3 through mineral weathering, so that the salt and alkali ions are reduced, and simultaneously, the microelements of potassium, phosphorus, magnesium, zinc, selenium and other nutrients are released, and the fixation of atmospheric CO2 is realized in the mineral weathering-carbonate precipitation process.\|[0003] In the technical development process, a field-scale silicate mineral leaching weathering experiment is a key link for verifying mineral improvement effect and carbon sequestration potential. The weathering, ion migration and salt replacement processes of minerals in the soil take soil water as a main reaction medium, and the changes of cations, anions, dissolved inorganic carbon and other components in the soil water can directly reflect the weathering rate, the carbon fixation reaction process and the salt migration condition of the minerals. However, the prior art generally relies on manually formulating water or groundwater as a drenching solution, or employing surface runoff sampling instead of in situ soil water collection, which results in:\| 1) The weathering reaction condition is distorted, namely the artificially prepared leaching solution cannot accurately reproduce the pH value, the ionic strength and the organic acid content of the soil in the microenvironment, and the reality of mineral dissolution and carbonate precipitation reaction is affected; \| 2) The salt migration data is inaccurate, namely, the surface water sample is often influenced by evaporation, precipitation and surface pollution, and the real migration state of the salt with different depths of the section is difficult to reflect; \| 3) The carbon fixation amount has distortion and deviation, namely, the key indexes such as Dissolved Inorganic Carbon (DIC) and bicarbonate (HCO 3 -) in the in-situ soil water are lacked, so that the evaluation error of the carbon fixation amount is large. \|[0004] Therefore, in the research and product development of enhancing silicate mineral weathering for improvement of salty soil and carbon fixation, there is a need for a technical scheme capable of efficiently collecting real soil water samples under the condition of not damaging the in-situ structure and the moisture dynamics of soil so as to obtain reliable weathering reaction, salt replacement and carbon fixation process data and promote the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|[0005] The invention provides a buried soil water collecting system, which can collect soil water samples of different soil layers for a long time, stably and in situ under field conditions, and ensure that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for the mechanism research, the effect evaluation and the product optimization of the multifunctional silicate mineral conditioner in the application of improving and fixing the carbon of the saline soil.\|DISCLOSURE\|Disclosure of Invention\|[0006] Based on the above problems existing in the prior art, an object of the embodiments of the present invention is to provide a buried soil water collection system capable of efficiently collecting real soil water samples under the condition that the in-situ structure and the moisture dynamics of the soil are not damaged, so as to solve the technical problems in the prior art that soil water samples of different soil layers cannot be collected stably and in situ for a long time under the field condition, and chemical composition and hydraulic characteristics of the collected liquid are difficult to be ensured to be consistent with the soil environment.\|[0007] In order to achieve the above purpose, the invention adopts the technical scheme that the buried soil water collecting system comprises:\| A fixed bracket; \| The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; \| the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; \| The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; \| a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and \|The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.\|[0008] Further, the porous water absorbing material is a columnar sponge, the axial direction of the columnar sponge is parallel to the axial direction of the porous ceramic tube, and the outer peripheral surface of the columnar sponge is in contact with the inner side wall of the porous ceramic tube.\|[0009] Further, the extrusion assembly comprises a first abutting part arranged in the porous ceramic tube in a sliding manner, a second abutting part arranged in the porous ceramic tube in a sliding manner, an elastic part for elastically abutting the second abutting part towards the first abutting part, and a push-pull rod for driving the first abutting part to slide towards the second abutting part, wherein the first abutting part is arranged close to the closed end of the porous ceramic tube, the first abutting part is abutted against the first end of the columnar sponge, the second abutting part is arranged close to the opening end of the porous ceramic tube, the first abutting part is abutted against the second end of the columnar sponge, a first sliding hole for the push-pull rod to pass through is formed in the second abutting part, a second sliding hole for the push-pull rod to pass through is formed in the columnar sponge, the first end of the rod stretches into the porous ceramic tube through the opening end of the porous ceramic tube, and is connected with the first abutting part after sequentially passing through the first sliding hole and the second hole, and the first abutting part is connected with the second driving device.\|[0010] Further, the elastic piece is a spiral spring accommodated in the porous ceramic tube, an abutting cover for abutting against the spiral spring is arranged at the opening end of the porous ceramic tube, one end of the spiral spring abuts against and is fixed on the abutting cover, the other end of the spiral spring abuts against the second abutting piece, and a third sliding hole for the push-pull rod to pass through is formed in the abutting cover.\|[0011] Further, the first pressing piece comprises a first piston arranged in the porous ceramic tube in a sliding mode and a first pressing piece connected with the first piston, the outer peripheral surface of the first piston is in interference contact with the inner side wall of the porous ceramic tube, the first pressing piece is in interference contact with the first end of the columnar sponge, the second pressing piece comprises a second pressing piece connected with the second piston in the porous ceramic tube in a sliding mode, the outer peripheral surface of the second piston is in interference contact with the inner side wall of the porous ceramic tube, and the second pressing piece is in interference contact with the second end of the columnar sponge.\|[0012] Further, the porous ceramic pipe comprises a first pipe section and a second pipe section which are integrally formed, one end, away from the second pipe section, of the first pipe section is a closed end, one end, away from the first pipe section, of the second pipe section is an open end, a microporous structure capable of adsorbing and transmitting soil water is arranged on the pipe wall of the first pipe section, the first piston and the columnar sponge are located in the first pipe section, the pipe wall of the second pipe section is of an airtight and waterproof compact structure, the second piston and the elastic piece are located in the second pipe section, and the water outlet is formed in the pipe wall of the second pipe section.\|[0013] Further, the quantity of soil water adsorption components sets up to a plurality of, and is a plurality of soil water adsorption components just interval arrangement side by side, every soil water adsorption components is supporting to be set up one extrusion subassembly, every extrusion subassembly with drive arrangement links to each other.\|[0014] Further, the driving device comprises a sliding rod, a driving rod and a cylinder, wherein the two ends of the sliding rod are respectively arranged on the fixed support in a sliding mode, the driving rod is used for driving the sliding rod to move along the axial direction of the sliding rod, the cylinder is used for driving the driving rod to move along the axial direction, the axial direction of the sliding rod is perpendicular to the axial direction of the sliding rod, the second end of the sliding rod is connected with the sliding rod, the axial direction of the driving rod is parallel to the axial direction of the sliding rod, the first end of the driving rod is connected with the centering position of the sliding rod, and the second end of the driving rod is connected with a piston rod of the cylinder.\|[0015] Further, the number of the cylinders is two, piston rods of the two cylinders are symmetrically distributed by taking a central axis of the driving rod as a symmetrical axis, the driving device further comprises a connecting rod axially perpendicular to the axial direction of the driving rod and two pulley blocks symmetrically arranged on two sides of the driving rod, pull ropes are wound on each pulley block, the axial direction of a vertical section of each pull rope is parallel to the axial direction of the driving rod, one pull rope connects a first end of the sliding rod with a first end of the connecting rod, the other pull rope connects a second end of the sliding rod with a second end of the connecting rod, two ends of the connecting rod are respectively connected with corresponding piston rods, and the second end of the driving rod is connected with a centering position of the connecting rod.\|[0016] Further, the filter layer comprises at least one layer of non-woven fabrics or silt filter screens.\|[0017] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:\| According to the buried soil water collecting system provided by the embodiment of the invention, the porous ceramic pipe with the pipe wall having the micropore structure is buried in soil, the porous ceramic pipe is internally provided with the porous water absorbing material capable of absorbing and storing soil water and the extrusion component capable of extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic pipe under the capillary action, and is absorbed and transmitted to the porous water absorbing material through the micropore structure of the porous ceramic pipe, so that the porous water absorbing material can continuously absorb and store the soil water. And when the water storage amount in the porous water absorbing material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorbing material, so that the soil water stored in the porous water absorbing material is extruded, and the extruded soil water is drained to the water storage container through the water outlet holes and the liquid guide tube on the porous ceramic tube, so that the soil water is stored in the water storage container in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation. \|DRAWINGS DESCRIPTION\|[0018] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0019] FIG. 1 is a schematic perspective view of a buried soil water collection system according to the present invention;\| FIG. 2 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; \| FIG. 3 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; \| FIG. 4 is a schematic view of a buried soil water collection system according to the present invention buried in soil; \| FIG. 5 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in an uncompressed state according to the present invention; \| FIG. 6 is a cross-sectional view of the soil water adsorbing assembly and squeeze assembly of the present invention in an uncompressed state; \| FIG. 7 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in a squeezed state according to the present invention; \| FIG. 8 is a cross-sectional view of the soil water adsorbing assembly and the squeezing assembly according to the present invention in a squeezed state; \| fig. 9 is an exploded view of a soil water adsorbing assembly and a squeezing assembly according to the present invention. \|[0020] Wherein, each reference sign in the figure:\| 1-a fixed bracket, 11-a sliding groove; \| 2-a soil water adsorption component, 21-a porous ceramic tube, 211-a first tube section, 212-a second tube section, 213-a water outlet hole, 22-a porous water absorbing material, 221-a second sliding hole, 23-a supporting cover and 231-a third sliding hole; \| 3-extrusion assembly, 31-first pressing piece, 311-first piston, 312-first pressing piece, 32-second pressing piece, 321-second piston, 322-second pressing piece, 323-first sliding hole, 33-elastic piece and 34-push-pull rod; \| 4-driving device, 41-sliding rod, 42-driving rod, 43-cylinder, 431-piston rod, 44-pulley block, 441-fixed pulley, 442-movable pulley, 45-pull rope, 451-vertical section, 46-first pulley bracket, 47-second pulley bracket, 48-sliding chute or bar-shaped sliding hole and 49-connecting rod; \| a 5-liquid collecting system, a 51-water storage container, a 52-liquid guiding tube; \| 6-soil profile and 7-sliding shaft. \|INVENTION MODE\|Detailed Description\|[0021] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0022] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," "third," and "fourth" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first", "a second", "a third", and "a fourth" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0023] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.\|[0024] Referring to fig. 1 to 9, a description will be given of a buried soil water collecting system according to an embodiment of the present invention. Referring to fig. 1, 2 and 3 in combination, the buried soil water collecting system according to the embodiment of the present invention includes a fixing bracket 1, a soil water adsorbing assembly 2, an extruding assembly 3, a driving device 4, a liquid collecting system 5 and a filtering layer, wherein the fixing bracket 1 is used for fixing on one side of a soil profile 6, and is mainly used for supporting and fixing the whole buried soil water collecting system. The soil water adsorption assembly 2 is capable of adsorbing and storing soil water in soil by capillary action, the soil water adsorption assembly 2 comprises a porous ceramic tube 21 for burying the soil and a porous water absorbing material 22 arranged in the porous ceramic tube 21, a first end of the porous ceramic tube 21 is a closed end, the closed end of the porous ceramic tube 21 is in a conical structure so as to facilitate the insertion of the porous ceramic tube 21 into the soil, and a second end of the porous ceramic tube 21 is an open end. The position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is detachably connected or fixedly connected with the fixed support 1, and the position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is provided with a water outlet hole 213, and the water outlet hole 213 is communicated with the inner cavity of the porous ceramic tube 21. The porous ceramic tube 21 has a microporous structure on the wall, which can adsorb and transfer soil water in soil to the porous water absorbing material 22 by capillary action, the porous water absorbing material 22 has a continuous and mutually penetrating porous structure inside, and the porous water absorbing material 22 can adsorb and store a certain volume of soil water. The porous ceramic tube 21 has a cylindrical structure, and can ensure a maximum area of contact with the soil. Meanwhile, the porous water absorbing material 22 has a cylindrical structure, and can ensure contact with the inner tube wall of the porous ceramic tube 21 at a maximum area.\|[0025] The extrusion component 3 is movably arranged in the porous ceramic tube 21, and the extrusion component 3 is used for extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22, so that soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water flows out of the porous ceramic tube 21 through the water outlet holes 213 on the porous ceramic tube 21. The driving device 4 is arranged on the fixed bracket 1, the driving device 4 is connected with the extrusion assembly 3, and the driving device 4 is used for driving the extrusion assembly 3 to extrude the porous water absorbing material 22 according to a preset program or periodically, so that soil water stored in a continuous porous structure of the porous water absorbing material 22 is extruded. The liquid collecting system 5 includes a water storage container 51 for collecting soil water and a liquid guide tube 52 connecting the water storage container 51 with the water outlet 213, and the soil water flowing out through the water outlet 213 can be concentrated and stored in the water storage container 51 by drainage of the liquid guide tube 52. The filter layer wraps the outer side of the porous ceramic tube 21, and can allow soil water to permeate into the microporous structure of the porous ceramic tube 21, and meanwhile, the filter layer can block sediment in soil on the outer side of the porous ceramic tube 21, so that sediment in soil is blocked to block the microporous structure of the porous ceramic tube 21.\|[0026] Referring to fig. 4, a vertical section is excavated on one side of the soil to be taken, a porous ceramic tube 21 of a soil water adsorption component 2 is transversely inserted or buried into the soil through a soil section 6, a fixing support 1 is fixed on one side of the soil section 6, so that the porous ceramic tube 21 of the soil water adsorption component 2 cannot relatively displace with the soil, and a waterproof and airtight sealing film is paved on the soil surface and the soil section 6, wherein the sealing film can be, but is not limited to, a plastic film. In this way, the water (soil water) absorbed in the soil can permeate the filter layer, under the capillary action, the water is absorbed by the micropore structure of the porous ceramic tube 21 and is transmitted to the porous water absorbing material 22, the porous water absorbing material 22 continuously absorbs the soil water and continuously stores the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22, when the water storage capacity in the porous water absorbing material 22 reaches a certain value, the water storage capacity in the porous water absorbing material 22 can transmit a signal to the controller through the humidity sensor and/or the water content sensor, the controller controls the driving device 4 to work according to a preset program after receiving the signal, the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, and the soil water is concentrated and stored in the water storage container 51. After the soil water in the porous water absorbing material 22 is fully extruded, the controller controls the driving device 4 to stop working, at this time, the extrusion assembly 3 finishes the extrusion action on the porous water absorbing material 22, the porous water absorbing material 22 can recover the original state, continuously absorb the soil water again, and continuously store the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22 until the water storage amount in the porous water absorbing material 22 reaches a certain value, the controller can transmit signals to the controller through the humidity sensor and/or the water content sensor, after receiving the signals, the controller controls the driving device 4 to work according to a preset program, and the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded.\|[0027] Compared with the prior art, the buried soil water collecting system provided by the embodiment of the invention has the advantages that the porous ceramic tube 21 with the wall having the micropore structure is buried in soil, the porous water absorbing material 22 capable of absorbing and storing soil water and the extrusion component 3 capable of extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22 are arranged in the porous ceramic tube 21, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic tube 21 under the capillary action, and is absorbed and transmitted to the porous water absorbing material 22 through the micropore structure of the porous ceramic tube 21, so that the porous water absorbing material 22 can continuously absorb and store the soil water. Until the water storage amount in the porous water absorbing material 22 is sufficient, the squeezing component 3 is driven by the driving device 4 to squeeze the porous water absorbing material 22, so that the soil water stored in the porous water absorbing material 22 is squeezed out, and the squeezed soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, so that the soil water is stored in the water storage container 51 in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation.\|[0028] Referring to fig. 6, 8 and 9 in combination, in some embodiments, the porous water absorbing material 22 is a cylindrical sponge, the axial direction of the cylindrical sponge is parallel to the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the cylindrical sponge is in contact with the inner side wall of the porous ceramic tube 21. In this embodiment, the porous water absorbing material 22 is preferably a sponge with good water absorbing and storing properties, and the sponge is arranged in the porous ceramic tube 21 in a columnar shape, so that the axial direction of the columnar sponge is consistent with the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the columnar sponge is contacted with the inner side wall of the porous ceramic tube 21, thereby ensuring that the columnar sponge is contacted with the inner tube wall of the porous ceramic tube 21 in the largest area, and improving the adsorption and collection effects of soil water. In addition, the sponge is arranged in the porous ceramic tube 21 in a columnar shape, and is compressed from the axial direction of the columnar sponge through the extrusion component 3, so that on one hand, the compression ratio of the columnar sponge can be increased to fully extrude soil water in the columnar sponge, and the adsorption and collection efficiency of the soil water can be further improved, and on the other hand, when the extrusion component 3 finishes extrusion action on the columnar sponge, the columnar sponge is favorable for quickly recovering the original state, and then the soil water can be better adsorbed and stored later. The porous absorbent material 22 may be, but is not limited to, a sponge, and the porous absorbent material 22 may also be a porous material having a certain compression ratio, such as absorbent cotton, nonwoven fabric, or the like.\|[0029] Referring to fig. 6, 8 and 9, in some embodiments, the pressing assembly 3 includes a first pressing member 31 slidably disposed in the porous ceramic tube 21, a second pressing member 32 slidably disposed in the porous ceramic tube 21, an elastic member 33 for elastically pressing the second pressing member 32 toward the first pressing member 31, and a push-pull rod 34 for driving the first pressing member 31 to slide toward the second pressing member 32, wherein the first pressing member 31 is disposed adjacent to the closed end of the porous ceramic tube 21, the first pressing member 31 abuts against a first end of the columnar sponge, the second pressing member 32 is disposed adjacent to the open end of the porous ceramic tube 21, the first pressing member 31 abuts against a second end of the columnar sponge, a first sliding hole 323 for the push-pull rod 34 to pass through is disposed on the second pressing member 32, a second sliding hole 221 for the push-pull rod 34 to pass through is disposed on the columnar sponge, the first end of the rod 34 extends into the porous ceramic tube 21 through the open end of the porous ceramic tube 21, and is connected to the first sliding hole 323 and the second sliding hole 221 after sequentially passing through the first sliding hole and the second sliding hole 221, and the second pressing member 31 abuts against a second end of the columnar sponge, and the second end of the rod 34 is connected to the driving device 4. In this embodiment, the driving device 4 pulls the push-pull rod 34 towards the open end of the porous ceramic tube 21, the push-pull rod 34 drives the first pressing member 31 to move towards the second pressing member 32, and as the distance between the first pressing member 31 and the second pressing member 32 gradually decreases, the columnar sponge between the first pressing member 31 and the second pressing member 32 is continuously compressed, and the soil water in the columnar sponge is also continuously extruded in the compression process. In the process of pressing the columnar sponge by the first pressing piece 31 and the second pressing piece 32, the second pressing piece 32 is elastically pressed against the first pressing piece 31 by the elastic piece 33, so that soil water in the columnar sponge is slowly released under the elastic buffering action of the elastic piece 33, the columnar sponge is prevented from being excessively compressed by the first pressing piece 31 and the second pressing piece 32 instantly, the pressure in the porous ceramic tube 21 is instantly increased, the soil water can leak through the micropore structure of the porous ceramic, and the pH value and the ion concentration in the soil water can be changed. Because be equipped with the second slide hole 221 that supplies push-and-pull rod 34 to pass on the column sponge, the column sponge passes through second slide hole 221 cover and locates on the push-and-pull rod 34, in the in-process of first pressure piece 31 and the extrusion of second pressure piece 32 column sponge, not only can effectively avoid the column sponge that axial length is longer to take place distortion, can be favorable to the column sponge later stage to resume original state fast moreover. It should be noted that, a sealing ring is disposed between the push-pull rod 34 and the first sliding hole 323 to enhance the sealing performance of the sliding contact between the push-pull rod 34 and the first sliding hole 323. In addition, locate the column sponge between first pressure piece 31 and the second pressure piece 32 to push up the elasticity of second pressure piece 32 towards first pressure piece 31 through elastic component 33, on the one hand be favorable to high efficiency with the soil water extrusion in the column sponge, on the other hand can push back the column sponge to the position that adsorbs the soil water through the action of pushing up of elastic component 33 fast through the second pressure piece 32.\|[0030] Referring to fig. 5, 8 and 9 in combination, in some embodiments, the elastic member 33 is a coil spring accommodated in the porous ceramic tube 21, the open end of the porous ceramic tube 21 is provided with a holding cover 23 for holding the coil spring, one end of the coil spring is held against and fixed on the holding cover 23, the other end of the coil spring is held against the second holding member 32, the holding cover 23 is provided with a third sliding hole 231 through which the push-pull rod 34 passes, and a sealing ring is disposed between the push-pull rod 34 and the third sliding hole 231 to enhance the sealing performance of sliding contact between the push-pull rod 34 and the third sliding hole 231. It should be noted that the holding cover 23 may be, but not limited to, connected to the open end of the porous ceramic tube 21 by a threaded connection, and the elastic member 33 may be, but not limited to, a coil spring.\|[0031] Referring to fig. 6, 8 and 9, in some embodiments, the first pressing member 31 includes a first piston 311 slidably disposed in the porous ceramic tube 21 and a first pressing member 312 connected to the first piston 311, the outer peripheral surface of the first piston 311 is in interference contact with the inner sidewall of the porous ceramic tube 21, the first pressing member 312 abuts against the first end of the cylindrical sponge, the first piston 311 is a rubber member or a silicone member having elasticity, the first pressing member 312 is a hard metal sheet or a plastic sheet, and a supporting and reinforcing effect is formed on the first piston 311 by the first pressing member 312, so as to prevent the first pressing member 31 from deforming during the process of pressing the cylindrical spring. Similarly, the second pressing member 32 includes a second pressing member 322 slidably disposed in the porous ceramic tube 21 and connected to the second piston 321, where the outer circumferential surface of the second piston 321 is in interference contact with the inner sidewall of the porous ceramic tube 21, the second pressing member 322 abuts against the second end of the cylindrical sponge, the second piston 321 is a rubber member or a silica gel member having elasticity, and the second pressing member 322 is a hard metal sheet or a plastic sheet, and forms a supporting and reinforcing effect on the second piston 321 by the second pressing member 322, so as to prevent the deformation of the first pressing member 31 in the process of pressing the cylindrical spring.\|[0032] Referring to fig. 7, 8 and 9 in combination, in some embodiments, the porous ceramic tube 21 includes a first tube section 211 and a second tube section 212 that are integrally formed, one end of the first tube section 211 away from the second tube section 212 is a closed end, one end of the second tube section 212 away from the first tube section 211 is an open end, a microporous structure capable of adsorbing and transmitting soil water is provided on a tube wall of the first tube section 211, the first piston 311 and the columnar sponge are located in the first tube section 211, and the soil water can be adsorbed and transmitted to the columnar sponge in the first tube section 211 by capillary action of the microporous structure. Meanwhile, the pipe wall of the second pipe section 212 is of a dense structure which is airtight and watertight, and the second piston 321 and the elastic piece 33 are located in the second pipe section 212, so that the elastic piece 33 in the second pipe section 212 cannot pollute soil water, and meanwhile, the soil water cannot flow into the second pipe section 212 to erode the elastic piece 33. It should be noted that, when the first pressing member 31 drives the columnar sponge into the second pipe section 212, the elastic member 33 is in a compressed state, and the elastic member 33 can elastically press the second pressing member 32 against the first pressing member 31, so that the second pressing member 32 cooperates with the first pressing member 31 to compress the columnar sponge into the sealed second pipe cavity, and the soil water extruded from the columnar sponge flows out through the water outlet 213 on the pipe wall of the second pipe section 212. In addition, when the second pressing member 32 compresses the columnar sponge in the sealed second lumen in cooperation with the first pressing member 31, the pressure in the second tube section 212 can be increased, so that the soil water in the second tube section 212 is pressed out, and the collection efficiency of the soil water can be accelerated.\|[0033] Referring to fig. 1, 2 and 3, in some embodiments, in order to collect soil water more quickly and efficiently, a plurality of soil water adsorbing assemblies 2 are arranged, and a plurality of soil water adsorbing assemblies 2 are arranged side by side and at intervals, and each soil water adsorbing assembly 2 is provided with a squeezing assembly 3 in a matching manner, and each squeezing assembly 3 is connected with a driving device 4.\|[0034] Referring to fig. 1, 2 and 3, in some embodiments, the driving device 4 includes a sliding rod 41 with two ends slidably disposed on the fixed support 1, a driving rod 42 for driving the sliding rod 41 to move along the axial direction of the push-pull rod 34, and an air cylinder 43 for driving the driving rod 42 to move along the axial direction, the fixed support 1 is provided with a sliding groove 11, and two ends of the sliding rod 41 are slidably inserted into the sliding groove 11. The axial direction of the sliding rod 41 is perpendicular to the axial direction of the sliding rod 34, the second end of the sliding rod 34 is connected with the sliding rod 41, the axial direction of the driving rod 42 is parallel to the axial direction of the sliding rod 34, the first end of the driving rod 42 is connected with the central position of the sliding rod 34, and the second end of the driving rod 42 is connected with a piston rod 431 of the air cylinder 43. In this embodiment, the push-pull rod 34 is driven to axially move by the telescopic movement of the piston rod 431 of the air cylinder 43, so that the driving rod 42 can be driven to axially move along the driving rod 42 by the push-pull rod 34, the sliding rod 41 further drives the push-pull rod 34 to axially move, and the push-pull rod 34 drives the first pressing member 31 to reciprocate along the axial direction of the porous ceramic tube 21, so that the columnar sponge can be pressed by the first pressing member 31 and the second pressing member 32. It should be noted that, the fixed bracket 1 is provided with a sliding slot, two ends of the sliding rod 41 are respectively disposed in the corresponding sliding slots, the fixed bracket 1 is further provided with a fourth sliding hole, and the driving shaft is slidably inserted into the fourth sliding hole.\|[0035] Referring to fig. 1,2 and 3 in combination, in some embodiments, in order to enhance the stability of the movement of the push-pull rod 34 driven by the driving device 4 and to maintain the high precision operation of the push-pull rod 34, the number of the air cylinders 43 is two, the piston rods 431 of the two air cylinders 43 are symmetrically distributed with the central axis of the driving rod 42 as a symmetrical axis, the driving device 4 further comprises a connecting rod 49 axially perpendicular to the axial direction of the push-pull rod 34 and two pulley blocks 44 symmetrically arranged at two sides of the driving rod 42, each pulley block 44 is wound with a pull rope 45, the axial direction of the vertical section 451 of each pull rope 45 is parallel to the axial direction of the push-pull rod 34, one pull rope 45 connects the first end of the sliding rod 41 with the first end of the connecting rod 49, the other pull rope 45 connects the second end of the sliding rod 41 with the second end of the connecting rod 49, and the two ends of the connecting rod 49 are respectively connected with the corresponding piston rods 431, and the second end of the driving rod 42 is connected with the central position of the connecting rod 49. It should be noted that, each pulley block 44 includes at least one fixed pulley 441 and at least one movable pulley 442, the fixed pulley 441 is rotatably disposed on the fixed bracket 1 through the first pulley bracket 46, the first pulley bracket 46 is fixedly connected with the fixed bracket 1, the movable pulley 442 is rotatably disposed on the fixed bracket 1 through the second pulley bracket 47, and the second pulley bracket 47 is fixedly connected with the fixed bracket 1. Specifically, the fixed support 1 is provided with a second pulley support 47, the second pulley support 47 is provided with a sliding groove or a bar-shaped sliding hole 48 capable of guiding the movable pulley 442 to slide along the axial direction of the driving rod 42, and two sections of sliding shafts 7 respectively inserted into the sliding groove or the bar-shaped sliding hole 48, and the movable pulley 442 is slidably arranged on the guiding support 48 through a sliding matching structure of the sliding shafts 7 and the sliding groove or the bar-shaped sliding hole 48.\|[0036] It will be appreciated that in some embodiments, the filter layer comprises at least one layer of non-woven fabric, because the non-woven fabric has the advantages of being flexible, light in weight, non-toxic, easy to decompose, low in cost, and the like, the porous ceramic tube 21 can be effectively wrapped by the non-woven fabric as the filter layer, so that the pollution to soil water is avoided, the pollution to soil is low, and meanwhile, the cost of the buried soil water collecting system can be effectively controlled. Of course, the filter layer may also include at least one layer of sediment filter screen, and the filter layer may also be in other structural forms capable of blocking sediment outside the filter layer. It should be noted that the filter layer includes at least one layer of non-woven fabric or silt filter screen, which means that the filter layer wrapped on the outer side of the porous ceramic tube 21 may be a layer structure or a multi-layer structure, and is determined according to the filtering effects of different filtering materials and structures.\|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.	(CN121253236)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reclamation and treatment, and particularly relates to a buried soil water collection system.\|BACKGROUND ART\|[0002] China is a large country of saline-alkali soil, and the third country is the first 10 countries in the area of saline-alkali soil. The Chinese saline-alkali soil is distributed in 17 provinces including northwest, northeast, north China and coastal areas, the total area of the saline-alkali barren lands and the saline-alkali lands affecting the cultivated lands exceeds 5 hundred million mu, and the agricultural production and the ecological safety are seriously restricted. In order to respond to the requirements of comprehensive treatment and comprehensive utilization of saline-alkali soil with stable promotion, development of a multifunctional silicate mineral conditioner with functions of improving saline-alkali soil, supplementing trace elements and fixing carbon is needed. The conditioner relies on the technology of enhancing silicate mineral weathering, and releases Ca 2+、Mg2+ and other exchange reactions Na +、CO2- 3、HCO-3 through mineral weathering, so that the salt and alkali ions are reduced, and simultaneously, the microelements of potassium, phosphorus, magnesium, zinc, selenium and other nutrients are released, and the fixation of atmospheric CO2 is realized in the mineral weathering-carbonate precipitation process.\|[0003] In the technical development process, a field-scale silicate mineral leaching weathering experiment is a key link for verifying mineral improvement effect and carbon sequestration potential. The weathering, ion migration and salt replacement processes of minerals in the soil take soil water as a main reaction medium, and the changes of cations, anions, dissolved inorganic carbon and other components in the soil water can directly reflect the weathering rate, the carbon fixation reaction process and the salt migration condition of the minerals. However, the prior art generally relies on manually formulating water or groundwater as a drenching solution, or employing surface runoff sampling instead of in situ soil water collection, which results in:\| 1) The weathering reaction condition is distorted, namely the artificially prepared leaching solution cannot accurately reproduce the pH value, the ionic strength and the organic acid content of the soil in the microenvironment, and the reality of mineral dissolution and carbonate precipitation reaction is affected; \| 2) The salt migration data is inaccurate, namely, the surface water sample is often influenced by evaporation, precipitation and surface pollution, and the real migration state of the salt with different depths of the section is difficult to reflect; \| 3) The carbon fixation amount has distortion and deviation, namely, the key indexes such as Dissolved Inorganic Carbon (DIC) and bicarbonate (HCO 3 -) in the in-situ soil water are lacked, so that the evaluation error of the carbon fixation amount is large. \|[0004] Therefore, in the research and product development of enhancing silicate mineral weathering for improvement of salty soil and carbon fixation, there is a need for a technical scheme capable of efficiently collecting real soil water samples under the condition of not damaging the in-situ structure and the moisture dynamics of soil so as to obtain reliable weathering reaction, salt replacement and carbon fixation process data and promote the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|[0005] The invention provides a buried soil water collecting system, which can collect soil water samples of different soil layers for a long time, stably and in situ under field conditions, and ensure that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for the mechanism research, the effect evaluation and the product optimization of the multifunctional silicate mineral conditioner in the application of improving and fixing the carbon of the saline soil.\|DISCLOSURE\|Disclosure of Invention\|[0006] Based on the above problems existing in the prior art, an object of the embodiments of the present invention is to provide a buried soil water collection system capable of efficiently collecting real soil water samples under the condition that the in-situ structure and the moisture dynamics of the soil are not damaged, so as to solve the technical problems in the prior art that soil water samples of different soil layers cannot be collected stably and in situ for a long time under the field condition, and chemical composition and hydraulic characteristics of the collected liquid are difficult to be ensured to be consistent with the soil environment.\|[0007] In order to achieve the above purpose, the invention adopts the technical scheme that the buried soil water collecting system comprises:\| A fixed bracket; \| The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; \| the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; \| The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; \| a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and \|The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.\|[0008] Further, the porous water absorbing material is a columnar sponge, the axial direction of the columnar sponge is parallel to the axial direction of the porous ceramic tube, and the outer peripheral surface of the columnar sponge is in contact with the inner side wall of the porous ceramic tube.\|[0009] Further, the extrusion assembly comprises a first abutting part arranged in the porous ceramic tube in a sliding manner, a second abutting part arranged in the porous ceramic tube in a sliding manner, an elastic part for elastically abutting the second abutting part towards the first abutting part, and a push-pull rod for driving the first abutting part to slide towards the second abutting part, wherein the first abutting part is arranged close to the closed end of the porous ceramic tube, the first abutting part is abutted against the first end of the columnar sponge, the second abutting part is arranged close to the opening end of the porous ceramic tube, the first abutting part is abutted against the second end of the columnar sponge, a first sliding hole for the push-pull rod to pass through is formed in the second abutting part, a second sliding hole for the push-pull rod to pass through is formed in the columnar sponge, the first end of the rod stretches into the porous ceramic tube through the opening end of the porous ceramic tube, and is connected with the first abutting part after sequentially passing through the first sliding hole and the second hole, and the first abutting part is connected with the second driving device.\|[0010] Further, the elastic piece is a spiral spring accommodated in the porous ceramic tube, an abutting cover for abutting against the spiral spring is arranged at the opening end of the porous ceramic tube, one end of the spiral spring abuts against and is fixed on the abutting cover, the other end of the spiral spring abuts against the second abutting piece, and a third sliding hole for the push-pull rod to pass through is formed in the abutting cover.\|[0011] Further, the first pressing piece comprises a first piston arranged in the porous ceramic tube in a sliding mode and a first pressing piece connected with the first piston, the outer peripheral surface of the first piston is in interference contact with the inner side wall of the porous ceramic tube, the first pressing piece is in interference contact with the first end of the columnar sponge, the second pressing piece comprises a second pressing piece connected with the second piston in the porous ceramic tube in a sliding mode, the outer peripheral surface of the second piston is in interference contact with the inner side wall of the porous ceramic tube, and the second pressing piece is in interference contact with the second end of the columnar sponge.\|[0012] Further, the porous ceramic pipe comprises a first pipe section and a second pipe section which are integrally formed, one end, away from the second pipe section, of the first pipe section is a closed end, one end, away from the first pipe section, of the second pipe section is an open end, a microporous structure capable of adsorbing and transmitting soil water is arranged on the pipe wall of the first pipe section, the first piston and the columnar sponge are located in the first pipe section, the pipe wall of the second pipe section is of an airtight and waterproof compact structure, the second piston and the elastic piece are located in the second pipe section, and the water outlet is formed in the pipe wall of the second pipe section.\|[0013] Further, the quantity of soil water adsorption components sets up to a plurality of, and is a plurality of soil water adsorption components just interval arrangement side by side, every soil water adsorption components is supporting to be set up one extrusion subassembly, every extrusion subassembly with drive arrangement links to each other.\|[0014] Further, the driving device comprises a sliding rod, a driving rod and a cylinder, wherein the two ends of the sliding rod are respectively arranged on the fixed support in a sliding mode, the driving rod is used for driving the sliding rod to move along the axial direction of the sliding rod, the cylinder is used for driving the driving rod to move along the axial direction, the axial direction of the sliding rod is perpendicular to the axial direction of the sliding rod, the second end of the sliding rod is connected with the sliding rod, the axial direction of the driving rod is parallel to the axial direction of the sliding rod, the first end of the driving rod is connected with the centering position of the sliding rod, and the second end of the driving rod is connected with a piston rod of the cylinder.\|[0015] Further, the number of the cylinders is two, piston rods of the two cylinders are symmetrically distributed by taking a central axis of the driving rod as a symmetrical axis, the driving device further comprises a connecting rod axially perpendicular to the axial direction of the driving rod and two pulley blocks symmetrically arranged on two sides of the driving rod, pull ropes are wound on each pulley block, the axial direction of a vertical section of each pull rope is parallel to the axial direction of the driving rod, one pull rope connects a first end of the sliding rod with a first end of the connecting rod, the other pull rope connects a second end of the sliding rod with a second end of the connecting rod, two ends of the connecting rod are respectively connected with corresponding piston rods, and the second end of the driving rod is connected with a centering position of the connecting rod.\|[0016] Further, the filter layer comprises at least one layer of non-woven fabrics or silt filter screens.\|[0017] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:\| According to the buried soil water collecting system provided by the embodiment of the invention, the porous ceramic pipe with the pipe wall having the micropore structure is buried in soil, the porous ceramic pipe is internally provided with the porous water absorbing material capable of absorbing and storing soil water and the extrusion component capable of extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic pipe under the capillary action, and is absorbed and transmitted to the porous water absorbing material through the micropore structure of the porous ceramic pipe, so that the porous water absorbing material can continuously absorb and store the soil water. And when the water storage amount in the porous water absorbing material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorbing material, so that the soil water stored in the porous water absorbing material is extruded, and the extruded soil water is drained to the water storage container through the water outlet holes and the liquid guide tube on the porous ceramic tube, so that the soil water is stored in the water storage container in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation. \|DRAWINGS DESCRIPTION\|[0018] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0019] FIG. 1 is a schematic perspective view of a buried soil water collection system according to the present invention;\| FIG. 2 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; \| FIG. 3 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; \| FIG. 4 is a schematic view of a buried soil water collection system according to the present invention buried in soil; \| FIG. 5 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in an uncompressed state according to the present invention; \| FIG. 6 is a cross-sectional view of the soil water adsorbing assembly and squeeze assembly of the present invention in an uncompressed state; \| FIG. 7 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in a squeezed state according to the present invention; \| FIG. 8 is a cross-sectional view of the soil water adsorbing assembly and the squeezing assembly according to the present invention in a squeezed state; \| fig. 9 is an exploded view of a soil water adsorbing assembly and a squeezing assembly according to the present invention. \|[0020] Wherein, each reference sign in the figure:\| 1-a fixed bracket, 11-a sliding groove; \| 2-a soil water adsorption component, 21-a porous ceramic tube, 211-a first tube section, 212-a second tube section, 213-a water outlet hole, 22-a porous water absorbing material, 221-a second sliding hole, 23-a supporting cover and 231-a third sliding hole; \| 3-extrusion assembly, 31-first pressing piece, 311-first piston, 312-first pressing piece, 32-second pressing piece, 321-second piston, 322-second pressing piece, 323-first sliding hole, 33-elastic piece and 34-push-pull rod; \| 4-driving device, 41-sliding rod, 42-driving rod, 43-cylinder, 431-piston rod, 44-pulley block, 441-fixed pulley, 442-movable pulley, 45-pull rope, 451-vertical section, 46-first pulley bracket, 47-second pulley bracket, 48-sliding chute or bar-shaped sliding hole and 49-connecting rod; \| a 5-liquid collecting system, a 51-water storage container, a 52-liquid guiding tube; \| 6-soil profile and 7-sliding shaft. \|INVENTION MODE\|Detailed Description\|[0021] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0022] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," "third," and "fourth" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first", "a second", "a third", and "a fourth" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0023] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.\|[0024] Referring to fig. 1 to 9, a description will be given of a buried soil water collecting system according to an embodiment of the present invention. Referring to fig. 1, 2 and 3 in combination, the buried soil water collecting system according to the embodiment of the present invention includes a fixing bracket 1, a soil water adsorbing assembly 2, an extruding assembly 3, a driving device 4, a liquid collecting system 5 and a filtering layer, wherein the fixing bracket 1 is used for fixing on one side of a soil profile 6, and is mainly used for supporting and fixing the whole buried soil water collecting system. The soil water adsorption assembly 2 is capable of adsorbing and storing soil water in soil by capillary action, the soil water adsorption assembly 2 comprises a porous ceramic tube 21 for burying the soil and a porous water absorbing material 22 arranged in the porous ceramic tube 21, a first end of the porous ceramic tube 21 is a closed end, the closed end of the porous ceramic tube 21 is in a conical structure so as to facilitate the insertion of the porous ceramic tube 21 into the soil, and a second end of the porous ceramic tube 21 is an open end. The position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is detachably connected or fixedly connected with the fixed support 1, and the position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is provided with a water outlet hole 213, and the water outlet hole 213 is communicated with the inner cavity of the porous ceramic tube 21. The porous ceramic tube 21 has a microporous structure on the wall, which can adsorb and transfer soil water in soil to the porous water absorbing material 22 by capillary action, the porous water absorbing material 22 has a continuous and mutually penetrating porous structure inside, and the porous water absorbing material 22 can adsorb and store a certain volume of soil water. The porous ceramic tube 21 has a cylindrical structure, and can ensure a maximum area of contact with the soil. Meanwhile, the porous water absorbing material 22 has a cylindrical structure, and can ensure contact with the inner tube wall of the porous ceramic tube 21 at a maximum area.\|[0025] The extrusion component 3 is movably arranged in the porous ceramic tube 21, and the extrusion component 3 is used for extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22, so that soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water flows out of the porous ceramic tube 21 through the water outlet holes 213 on the porous ceramic tube 21. The driving device 4 is arranged on the fixed bracket 1, the driving device 4 is connected with the extrusion assembly 3, and the driving device 4 is used for driving the extrusion assembly 3 to extrude the porous water absorbing material 22 according to a preset program or periodically, so that soil water stored in a continuous porous structure of the porous water absorbing material 22 is extruded. The liquid collecting system 5 includes a water storage container 51 for collecting soil water and a liquid guide tube 52 connecting the water storage container 51 with the water outlet 213, and the soil water flowing out through the water outlet 213 can be concentrated and stored in the water storage container 51 by drainage of the liquid guide tube 52. The filter layer wraps the outer side of the porous ceramic tube 21, and can allow soil water to permeate into the microporous structure of the porous ceramic tube 21, and meanwhile, the filter layer can block sediment in soil on the outer side of the porous ceramic tube 21, so that sediment in soil is blocked to block the microporous structure of the porous ceramic tube 21.\|[0026] Referring to fig. 4, a vertical section is excavated on one side of the soil to be taken, a porous ceramic tube 21 of a soil water adsorption component 2 is transversely inserted or buried into the soil through a soil section 6, a fixing support 1 is fixed on one side of the soil section 6, so that the porous ceramic tube 21 of the soil water adsorption component 2 cannot relatively displace with the soil, and a waterproof and airtight sealing film is paved on the soil surface and the soil section 6, wherein the sealing film can be, but is not limited to, a plastic film. In this way, the water (soil water) absorbed in the soil can permeate the filter layer, under the capillary action, the water is absorbed by the micropore structure of the porous ceramic tube 21 and is transmitted to the porous water absorbing material 22, the porous water absorbing material 22 continuously absorbs the soil water and continuously stores the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22, when the water storage capacity in the porous water absorbing material 22 reaches a certain value, the water storage capacity in the porous water absorbing material 22 can transmit a signal to the controller through the humidity sensor and/or the water content sensor, the controller controls the driving device 4 to work according to a preset program after receiving the signal, the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, and the soil water is concentrated and stored in the water storage container 51. After the soil water in the porous water absorbing material 22 is fully extruded, the controller controls the driving device 4 to stop working, at this time, the extrusion assembly 3 finishes the extrusion action on the porous water absorbing material 22, the porous water absorbing material 22 can recover the original state, continuously absorb the soil water again, and continuously store the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22 until the water storage amount in the porous water absorbing material 22 reaches a certain value, the controller can transmit signals to the controller through the humidity sensor and/or the water content sensor, after receiving the signals, the controller controls the driving device 4 to work according to a preset program, and the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded.\|[0027] Compared with the prior art, the buried soil water collecting system provided by the embodiment of the invention has the advantages that the porous ceramic tube 21 with the wall having the micropore structure is buried in soil, the porous water absorbing material 22 capable of absorbing and storing soil water and the extrusion component 3 capable of extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22 are arranged in the porous ceramic tube 21, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic tube 21 under the capillary action, and is absorbed and transmitted to the porous water absorbing material 22 through the micropore structure of the porous ceramic tube 21, so that the porous water absorbing material 22 can continuously absorb and store the soil water. Until the water storage amount in the porous water absorbing material 22 is sufficient, the squeezing component 3 is driven by the driving device 4 to squeeze the porous water absorbing material 22, so that the soil water stored in the porous water absorbing material 22 is squeezed out, and the squeezed soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, so that the soil water is stored in the water storage container 51 in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation.\|[0028] Referring to fig. 6, 8 and 9 in combination, in some embodiments, the porous water absorbing material 22 is a cylindrical sponge, the axial direction of the cylindrical sponge is parallel to the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the cylindrical sponge is in contact with the inner side wall of the porous ceramic tube 21. In this embodiment, the porous water absorbing material 22 is preferably a sponge with good water absorbing and storing properties, and the sponge is arranged in the porous ceramic tube 21 in a columnar shape, so that the axial direction of the columnar sponge is consistent with the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the columnar sponge is contacted with the inner side wall of the porous ceramic tube 21, thereby ensuring that the columnar sponge is contacted with the inner tube wall of the porous ceramic tube 21 in the largest area, and improving the adsorption and collection effects of soil water. In addition, the sponge is arranged in the porous ceramic tube 21 in a columnar shape, and is compressed from the axial direction of the columnar sponge through the extrusion component 3, so that on one hand, the compression ratio of the columnar sponge can be increased to fully extrude soil water in the columnar sponge, and the adsorption and collection efficiency of the soil water can be further improved, and on the other hand, when the extrusion component 3 finishes extrusion action on the columnar sponge, the columnar sponge is favorable for quickly recovering the original state, and then the soil water can be better adsorbed and stored later. The porous absorbent material 22 may be, but is not limited to, a sponge, and the porous absorbent material 22 may also be a porous material having a certain compression ratio, such as absorbent cotton, nonwoven fabric, or the like.\|[0029] Referring to fig. 6, 8 and 9, in some embodiments, the pressing assembly 3 includes a first pressing member 31 slidably disposed in the porous ceramic tube 21, a second pressing member 32 slidably disposed in the porous ceramic tube 21, an elastic member 33 for elastically pressing the second pressing member 32 toward the first pressing member 31, and a push-pull rod 34 for driving the first pressing member 31 to slide toward the second pressing member 32, wherein the first pressing member 31 is disposed adjacent to the closed end of the porous ceramic tube 21, the first pressing member 31 abuts against a first end of the columnar sponge, the second pressing member 32 is disposed adjacent to the open end of the porous ceramic tube 21, the first pressing member 31 abuts against a second end of the columnar sponge, a first sliding hole 323 for the push-pull rod 34 to pass through is disposed on the second pressing member 32, a second sliding hole 221 for the push-pull rod 34 to pass through is disposed on the columnar sponge, the first end of the rod 34 extends into the porous ceramic tube 21 through the open end of the porous ceramic tube 21, and is connected to the first sliding hole 323 and the second sliding hole 221 after sequentially passing through the first sliding hole and the second sliding hole 221, and the second pressing member 31 abuts against a second end of the columnar sponge, and the second end of the rod 34 is connected to the driving device 4. In this embodiment, the driving device 4 pulls the push-pull rod 34 towards the open end of the porous ceramic tube 21, the push-pull rod 34 drives the first pressing member 31 to move towards the second pressing member 32, and as the distance between the first pressing member 31 and the second pressing member 32 gradually decreases, the columnar sponge between the first pressing member 31 and the second pressing member 32 is continuously compressed, and the soil water in the columnar sponge is also continuously extruded in the compression process. In the process of pressing the columnar sponge by the first pressing piece 31 and the second pressing piece 32, the second pressing piece 32 is elastically pressed against the first pressing piece 31 by the elastic piece 33, so that soil water in the columnar sponge is slowly released under the elastic buffering action of the elastic piece 33, the columnar sponge is prevented from being excessively compressed by the first pressing piece 31 and the second pressing piece 32 instantly, the pressure in the porous ceramic tube 21 is instantly increased, the soil water can leak through the micropore structure of the porous ceramic, and the pH value and the ion concentration in the soil water can be changed. Because be equipped with the second slide hole 221 that supplies push-and-pull rod 34 to pass on the column sponge, the column sponge passes through second slide hole 221 cover and locates on the push-and-pull rod 34, in the in-process of first pressure piece 31 and the extrusion of second pressure piece 32 column sponge, not only can effectively avoid the column sponge that axial length is longer to take place distortion, can be favorable to the column sponge later stage to resume original state fast moreover. It should be noted that, a sealing ring is disposed between the push-pull rod 34 and the first sliding hole 323 to enhance the sealing performance of the sliding contact between the push-pull rod 34 and the first sliding hole 323. In addition, locate the column sponge between first pressure piece 31 and the second pressure piece 32 to push up the elasticity of second pressure piece 32 towards first pressure piece 31 through elastic component 33, on the one hand be favorable to high efficiency with the soil water extrusion in the column sponge, on the other hand can push back the column sponge to the position that adsorbs the soil water through the action of pushing up of elastic component 33 fast through the second pressure piece 32.\|[0030] Referring to fig. 5, 8 and 9 in combination, in some embodiments, the elastic member 33 is a coil spring accommodated in the porous ceramic tube 21, the open end of the porous ceramic tube 21 is provided with a holding cover 23 for holding the coil spring, one end of the coil spring is held against and fixed on the holding cover 23, the other end of the coil spring is held against the second holding member 32, the holding cover 23 is provided with a third sliding hole 231 through which the push-pull rod 34 passes, and a sealing ring is disposed between the push-pull rod 34 and the third sliding hole 231 to enhance the sealing performance of sliding contact between the push-pull rod 34 and the third sliding hole 231. It should be noted that the holding cover 23 may be, but not limited to, connected to the open end of the porous ceramic tube 21 by a threaded connection, and the elastic member 33 may be, but not limited to, a coil spring.\|[0031] Referring to fig. 6, 8 and 9, in some embodiments, the first pressing member 31 includes a first piston 311 slidably disposed in the porous ceramic tube 21 and a first pressing member 312 connected to the first piston 311, the outer peripheral surface of the first piston 311 is in interference contact with the inner sidewall of the porous ceramic tube 21, the first pressing member 312 abuts against the first end of the cylindrical sponge, the first piston 311 is a rubber member or a silicone member having elasticity, the first pressing member 312 is a hard metal sheet or a plastic sheet, and a supporting and reinforcing effect is formed on the first piston 311 by the first pressing member 312, so as to prevent the first pressing member 31 from deforming during the process of pressing the cylindrical spring. Similarly, the second pressing member 32 includes a second pressing member 322 slidably disposed in the porous ceramic tube 21 and connected to the second piston 321, where the outer circumferential surface of the second piston 321 is in interference contact with the inner sidewall of the porous ceramic tube 21, the second pressing member 322 abuts against the second end of the cylindrical sponge, the second piston 321 is a rubber member or a silica gel member having elasticity, and the second pressing member 322 is a hard metal sheet or a plastic sheet, and forms a supporting and reinforcing effect on the second piston 321 by the second pressing member 322, so as to prevent the deformation of the first pressing member 31 in the process of pressing the cylindrical spring.\|[0032] Referring to fig. 7, 8 and 9 in combination, in some embodiments, the porous ceramic tube 21 includes a first tube section 211 and a second tube section 212 that are integrally formed, one end of the first tube section 211 away from the second tube section 212 is a closed end, one end of the second tube section 212 away from the first tube section 211 is an open end, a microporous structure capable of adsorbing and transmitting soil water is provided on a tube wall of the first tube section 211, the first piston 311 and the columnar sponge are located in the first tube section 211, and the soil water can be adsorbed and transmitted to the columnar sponge in the first tube section 211 by capillary action of the microporous structure. Meanwhile, the pipe wall of the second pipe section 212 is of a dense structure which is airtight and watertight, and the second piston 321 and the elastic piece 33 are located in the second pipe section 212, so that the elastic piece 33 in the second pipe section 212 cannot pollute soil water, and meanwhile, the soil water cannot flow into the second pipe section 212 to erode the elastic piece 33. It should be noted that, when the first pressing member 31 drives the columnar sponge into the second pipe section 212, the elastic member 33 is in a compressed state, and the elastic member 33 can elastically press the second pressing member 32 against the first pressing member 31, so that the second pressing member 32 cooperates with the first pressing member 31 to compress the columnar sponge into the sealed second pipe cavity, and the soil water extruded from the columnar sponge flows out through the water outlet 213 on the pipe wall of the second pipe section 212. In addition, when the second pressing member 32 compresses the columnar sponge in the sealed second lumen in cooperation with the first pressing member 31, the pressure in the second tube section 212 can be increased, so that the soil water in the second tube section 212 is pressed out, and the collection efficiency of the soil water can be accelerated.\|[0033] Referring to fig. 1, 2 and 3, in some embodiments, in order to collect soil water more quickly and efficiently, a plurality of soil water adsorbing assemblies 2 are arranged, and a plurality of soil water adsorbing assemblies 2 are arranged side by side and at intervals, and each soil water adsorbing assembly 2 is provided with a squeezing assembly 3 in a matching manner, and each squeezing assembly 3 is connected with a driving device 4.\|[0034] Referring to fig. 1, 2 and 3, in some embodiments, the driving device 4 includes a sliding rod 41 with two ends slidably disposed on the fixed support 1, a driving rod 42 for driving the sliding rod 41 to move along the axial direction of the push-pull rod 34, and an air cylinder 43 for driving the driving rod 42 to move along the axial direction, the fixed support 1 is provided with a sliding groove 11, and two ends of the sliding rod 41 are slidably inserted into the sliding groove 11. The axial direction of the sliding rod 41 is perpendicular to the axial direction of the sliding rod 34, the second end of the sliding rod 34 is connected with the sliding rod 41, the axial direction of the driving rod 42 is parallel to the axial direction of the sliding rod 34, the first end of the driving rod 42 is connected with the central position of the sliding rod 34, and the second end of the driving rod 42 is connected with a piston rod 431 of the air cylinder 43. In this embodiment, the push-pull rod 34 is driven to axially move by the telescopic movement of the piston rod 431 of the air cylinder 43, so that the driving rod 42 can be driven to axially move along the driving rod 42 by the push-pull rod 34, the sliding rod 41 further drives the push-pull rod 34 to axially move, and the push-pull rod 34 drives the first pressing member 31 to reciprocate along the axial direction of the porous ceramic tube 21, so that the columnar sponge can be pressed by the first pressing member 31 and the second pressing member 32. It should be noted that, the fixed bracket 1 is provided with a sliding slot, two ends of the sliding rod 41 are respectively disposed in the corresponding sliding slots, the fixed bracket 1 is further provided with a fourth sliding hole, and the driving shaft is slidably inserted into the fourth sliding hole.\|[0035] Referring to fig. 1,2 and 3 in combination, in some embodiments, in order to enhance the stability of the movement of the push-pull rod 34 driven by the driving device 4 and to maintain the high precision operation of the push-pull rod 34, the number of the air cylinders 43 is two, the piston rods 431 of the two air cylinders 43 are symmetrically distributed with the central axis of the driving rod 42 as a symmetrical axis, the driving device 4 further comprises a connecting rod 49 axially perpendicular to the axial direction of the push-pull rod 34 and two pulley blocks 44 symmetrically arranged at two sides of the driving rod 42, each pulley block 44 is wound with a pull rope 45, the axial direction of the vertical section 451 of each pull rope 45 is parallel to the axial direction of the push-pull rod 34, one pull rope 45 connects the first end of the sliding rod 41 with the first end of the connecting rod 49, the other pull rope 45 connects the second end of the sliding rod 41 with the second end of the connecting rod 49, and the two ends of the connecting rod 49 are respectively connected with the corresponding piston rods 431, and the second end of the driving rod 42 is connected with the central position of the connecting rod 49. It should be noted that, each pulley block 44 includes at least one fixed pulley 441 and at least one movable pulley 442, the fixed pulley 441 is rotatably disposed on the fixed bracket 1 through the first pulley bracket 46, the first pulley bracket 46 is fixedly connected with the fixed bracket 1, the movable pulley 442 is rotatably disposed on the fixed bracket 1 through the second pulley bracket 47, and the second pulley bracket 47 is fixedly connected with the fixed bracket 1. Specifically, the fixed support 1 is provided with a second pulley support 47, the second pulley support 47 is provided with a sliding groove or a bar-shaped sliding hole 48 capable of guiding the movable pulley 442 to slide along the axial direction of the driving rod 42, and two sections of sliding shafts 7 respectively inserted into the sliding groove or the bar-shaped sliding hole 48, and the movable pulley 442 is slidably arranged on the guiding support 48 through a sliding matching structure of the sliding shafts 7 and the sliding groove or the bar-shaped sliding hole 48.\|[0036] It will be appreciated that in some embodiments, the filter layer comprises at least one layer of non-woven fabric, because the non-woven fabric has the advantages of being flexible, light in weight, non-toxic, easy to decompose, low in cost, and the like, the porous ceramic tube 21 can be effectively wrapped by the non-woven fabric as the filter layer, so that the pollution to soil water is avoided, the pollution to soil is low, and meanwhile, the cost of the buried soil water collecting system can be effectively controlled. Of course, the filter layer may also include at least one layer of sediment filter screen, and the filter layer may also be in other structural forms capable of blocking sediment outside the filter layer. It should be noted that the filter layer includes at least one layer of non-woven fabric or silt filter screen, which means that the filter layer wrapped on the outer side of the porous ceramic tube 21 may be a layer structure or a multi-layer structure, and is determined according to the filtering effects of different filtering materials and structures.\|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.	Family Number\|(117274553)\|117274553\|Object of Invention\|(CN121253236 A)\|The invention provides a buried soil water collecting system , which belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction and treatment , wherein a porous ceramic tube is buried in soil , a porous water absorbing material and an extrusion component for extruding the porous water absorbing material are arranged in the ( . . . ) \|Abstract\|(CN121253236 A)\|The invention provides a buried soil water collection system , and belongs to the technical field of rock weathering carbon sequestration and salinized soil transformation and governance , a porous ceramic tube is buried in soil , a porous water absorption material and an extrusion assembly for extruding the porous water absorption material are arranged in the porous ceramic tube , and soil water adsorbed in the soil is absorbed by the porous ceramic tube under the capillary action , so that the soil water is absorbed by the porous ceramic tube ; the soil water is adsorbed and transmitted to the porous water absorption material through the microporous structure of the porous ceramic tube , and the porous water absorption material can continuously adsorb and store the soil water . When the water storage amount in the porous water absorption material is sufficient , the extrusion assembly is driven by the driving device to extrude the porous water absorption material , so that the soil water stored in the porous water absorption material is extruded out , and the extruded soil water is drained to the water storage container through the water outlet holes in the porous ceramic pipe and the liquid guide pipe , so that the soil water is centrally stored in the water storage container . Therefore , the real soil water sample can be stably and efficiently collected for a long time under the field condition that the in - situ structure and the moisture dynamic state of the soil are not damaged . \|	Measurement	G01N-001/20\|G01N-001/20/35\|G01N-2001/2021\|G01N-2001/205		G01N-001/20\|G01N-001/20/35\|G01N-2001/2021\|G01N-2001/205	G01N-001/20	G01N-001/20										PENDING	(CN121253236)\|PENDING	ALIVE	(CN121253236)\|ALIVE	(CN121253236)\|LEGAL DETAILS FOR CN121253236\|Actual or expected expiration date=2045-10-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-10-29\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202511559558\|Application date=2025-10-29\|Standardized application number=2025CN-1559558\|Event publication date=2026-01-02\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN121253236\|Publication stage code=A\|Publication date=2026-01-02\|Standardized publication number=CN121253236\|Event publication date=2026-01-02\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2026-01-20\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN121253236)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKfJWdolE5dLe1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080386811&ekey=1806&xpn=CN121253236&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=gPZaP4yiAL%252BirZpns%252Bzw6pNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN121253236)\|CN	(CN121253236)\|NAME=LANZHOU UNIVERSITY , COUNTRY=CN		(CN121253236)\|NAME=HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=41028	(CN121253236)\|CN	(CN121253236)\|NAME=ZHANG JIETANG, COUNTRY=CN \|NAME=LI XINGYUAN\|NAME=GOU XIAOHUA	(CN121253236)\|9	1	1					(CN121253236)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2026-01-02\|Gazette number: GAZNUM=42-0101\|Number of Pages: NPAGES=21\|		(CN121253236)\|CHINESE (CHI)	(CN121253236)\|Patent	Titre: (CN121253236)\|Buried soil water collecting system Résumé: (CN121253236)\|The invention provides a buried soil water collection system, and belongs to the technical field of rock weathering carbon sequestration and salinized soil transformation and governance, a porous ceramic tube is buried in soil, a porous water absorption material and an extrusion assembly for extruding the porous water absorption material are arranged in the porous ceramic tube, and soil water adsorbed in the soil is absorbed by the porous ceramic tube under the capillary action, so that the soil water is absorbed by the porous ceramic tube; the soil water is adsorbed and transmitted to the porous water absorption material through the microporous structure of the porous ceramic tube, and the porous water absorption material can continuously adsorb and store the soil water. When the water storage amount in the porous water absorption material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorption material, so that the soil water stored in the porous water absorption material is extruded out, and the extruded soil water is drained to the water storage container through the water outlet holes in the porous ceramic pipe and the liquid guide pipe, so that the soil water is centrally stored in the water storage container. Therefore, the real soil water sample can be stably and efficiently collected for a long time under the field condition that the in-situ structure and the moisture dynamic state of the soil are not damaged.	19	Abstract	gpt-4o-mini	no	The article focuses on a soil water collection system and does not address accelerated weathering or CO₂ capture.
21	CN202210073314	CN202211317927\|CN202210073314	CN115445393\|CN115445393\|CN114522512	100174807	CN115445393 B 2024-04-26 [CN115445393B]\|CN115445393 A 2022-12-09 [CN115445393]\|CN114522512 A 2022-05-24 [CN114522512]	2022-01-21	2022-10-26\|2022-01-21	2024-04-26\|2022-12-09\|2022-05-24	(CN115445393B)\|2024-04-26\|	(CN115445393)\|2042-10-26\|(CN114522512)\|2022-12-06	(CN115445393)\|Method for improving carbon sink efficiency of soil and underground water	(CN115445393)\|The invention discloses a method for improving the carbon sink efficiency of soil and underground water, and relates to the technical field of carbon sink increase and carbon cycle improvement. The method comprises the following steps: step 1, judging and extracting a main rainfall infiltration supply area through site GIS analysis and DEM three-dimensional model, and taking the main rainfall infiltration supply area as an area for increasing the rainfall infiltration amount; step 2, paving peat soil with a high-adsorbability and high-water-content space to the area selected in the step 1, and wetting the dried peat soil with water before paving; thirdly, holes are formed in the laid peat soil, the permeability of a laid area is enhanced, more earth surface rainfall can enter the soil and underground water space through infiltration, and the CO2 amount adsorbed by the peat soil is increased. Through soil adsorption and rainfall infiltration leaching carrying processes, the content of dissolved inorganic carbon entering the soil and underground water is greatly increased, so that atmospheric CO2 is stored in a deep underground space, the carbon sequestration efficiency of the soil and underground water is improved, and important carbon sequestration significance is achieved.	GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN	(CN115445393)\|GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY ([CN])\|(CN115445393)\|GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY ([CN])\|(CN114522512)\|GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY ([CN])	YANG MINGXING\|ZHANG MIN\|YANG WU\|XIE FEI\|YAO DUNTING\|LI WEI	(CN115445393)\|YANG MINGXING\|ZHANG MIN\|YANG WU\|XIE FEI\|YAO DUNTING\|LI WEI\|(CN115445393)\|YANG MINGXING\|ZHANG MIN\|YANG WU\|XIE FEI\|YAO DUNTING\|LI WEI	(CN115445393)\|CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP)\|Reg. Nb: 11308\|(CN114522512)\|CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP)\|Reg. Nb: 11308	(CN115445393)\|Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.\|In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples.\|	(CN115445393)\|1. A method for improving the carbon sink efficiency of soil and underground water is characterized by comprising the following steps: the method comprises the following steps: Firstly, judging and extracting a main rainfall infiltration supplementing area through site GIS analysis and a DEM three-dimensional model to serve as an area for increasing rainfall infiltration; secondly, spreading peat soil with high adsorptivity and high water content to the area selected in the first step, and wetting the dried peat soil with water before spreading; thirdly, inserting holes in the peat soil which is well paved, enhancing the permeability of the paved area, and enabling more surface rainfall to enter soil and groundwater space through infiltration so as to increase the CO 2 absorbed by the peat soil; And fourthly, increasing the water infiltration amount by adopting a manual sprinkling or leaching mode in a rainfall-free season, increasing the CO 2 amount adsorbed by peat soil, and absorbing and storing atmospheric CO 2 in soil and underground water to form dissolved inorganic carbon so as to realize the purpose of carbon sink. \|	(CN115445393)\|The invention aims to provide a technology for improving carbon sink efficiency of soil and underground water, which is used for improving the carbon sink efficiency of the soil and the underground water for absorbing and storing CO 2 by improving the performance of the soil for absorbing CO 2 and according to the combination form of CO 2 and water in the surface process and the flow circulation mode, and solving the problems in the background technology.\|The invention discloses a method for improving carbon sink efficiency of soil and underground water, and relates to the technical field of carbon sink increasing and carbon circulation improving.\|The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps:\|	(CN115445393)\|GROUND(100,34)\|CARBON SINK(100,29)\|UNDERGROUND WATER(100,18)\|RAINFALL INFILTRATION(100,10)\|RAINFALL INFILTRATION REPLENISHMENT ZONE(66,1)\|RAINFALL INFILTRATION LEACHING(61,2)\|SPREADING PEAT SOIL(55,6)\|GROUNDWATER(45,12)\|SITE GI ANALYSIS(44,4)\|PEAT SOIL DRYING(43,6)\|PEAT SOIL(42,22)\|ADSORPTIVITY(40,6)\|SITE GI(37,4)\|INSERTION(36,4)\|SPRINKLING(36,1)\|SOIL PERFORMANCE(33,1)\|INFILTRATION(31,7)\|CARBON CIRCULATION(30,2)\|PAVED AREA(29,2)\|TILED PEAT SOIL(29,2)\|PEAT SOIL WETTING(28,2)\|SOIL CARBON SEQUESTRATION(25,1)\|LEACHING MODE(24,3)\|COLLECTION ZONE(22,1)\|RAINFALL FREE SEASON(21,3)\|SURFACE RAINFALL(19,6)\|DEM THREE DIMENSIONAL MODEL(18,4)\|HCO3 ION(18,4)\|CARBON SINK SIGNIFICANCE(18,2)\|PAVING THICKNESS(18,2)\|FLOW CIRCULATION MODE(17,1)\|GULLY(14,2)\|SOIL ADSORPTION(14,2)\|DEEP UNDERGROUND SPACE(13,4)\|DEPRESSION(12,4)\|WATER INFILTRATION(12,3)\|3D MODEL(11,4)\|DISSOLVED INORGANIC CARBON(10,15)\|PAVED REGION PERMEABILITY(10,2)\|SOIL RAINFALL INFILTRATION CHANNEL(10,1)\|RAINFALL INFILTRATION FLUSHING ACTION(9,1)\|RAINFALL SURFACE RUNOFF(8,7)\|SOIL PHYSICAL MODIFIER(8,2)\|DISSOLVED INORGANIC CARBON CONTENT(7,3)\|SOIL ADSORPTION CAPACITY(7,1)\|RAINFALL INFILTRATION SUPPLY AREA(6,4)\|WELL PAVED PEAT SOIL(6,2)\|ADSORPTIVE ABSORPTION(6,1)\|ATMOSPHERIC RAINFALL(6,1)\|CARBON SINK ECONOMIC PROSPECT(6,1)\|RAINFALL INFILTRATION REPLENISHMENT AREA(6,1)\|SOIL ADSORPTION PERFORMANCE(6,1)\|COLLECTION AREA(5,6)\|POROSITY(5,3)\|CARBON NEUTRALIZATION(5,2)\|FORMED INSERTION HOLE(5,2)\|SPRINKLING MODE(5,2)\|ECONOMY DEVELOPMENT(5,1)\|RAINFALL INFILTRATION CAPACITY(5,1)\|DITCH(4,2)\|SPREADING THICKNESS(4,2)\|STAINLESS STEEL STICK(4,2)\|\|(CN115445393)\|GROUND(100,44)\|UNDERGROUND WATER(100,26)\|CARBON SEQUESTRATION(100,13)\|PRECIPITATION INFILTRATION(100,1)\|LEAD PRECIPITATION INFILTRATION(89,1)\|SPREAD PEAT SOIL(84,4)\|RAINFALL INFILTRATION PERFORMANCE(83,1)\|SOLUTIONTHE INORGANIC CARBON(83,1)\|PERMEABILITY ENHANCEMENT(82,2)\|UNDERGROUND WATERTHE CARBON SEQUESTRATION(76,1)\|LEAD RAINFALL INFILTRATION(67,1)\|PEAT SOIL(63,21)\|PEAT SOIL DRYING(63,6)\|RECYCLING CARBON(60,1)\|RAINFALL(59,12)\|ADSORBABILITY(58,6)\|INFILTRATION(47,6)\|RAINFALL INFILTRATION RECHARGE AREA(47,1)\|GROUNDWATER CARBON SEQUESTRATION(46,1)\|SITE GI ANALYSIS(46,1)\|REPLENISHMENT AREA(44,2)\|TILED PEAT SOIL(43,2)\|FUNCTION MANUAL SPRINKLING(43,1)\|SOIL ADSORPTION(42,2)\|PEAT SOIL WETTING(41,2)\|ATMOSPHERIC RAINFALL(39,3)\|CARBON SEQUESTRATION SIGNIFICANCE(35,2)\|ADSORPTION FUNCTION(35,1)\|SPREADING PEAT SOIL(34,3)\|SPREADING AREA(33,2)\|GROUNDWATER(32,3)\|MODE FUNCTION MANUAL SPRINKLING(32,1)\|DEM THREE DIMENSIONAL MODEL(27,4)\|FLOW CIRCULATION MODE(26,1)\|GROUND SURFACE(25,6)\|CARBON SINK(22,25)\|SPREADING THICKNESS(22,3)\|EFFICIENCY FUNCTION(22,2)\|JIG(21,2)\|CARBON SEQUESTRATION EFFICIENCY FUNCTION(21,1)\|RAINFALL INFILTRATION ELUVIATION(20,1)\|GULLY(19,4)\|RAINFALL INFILTRATION REPLENISHMENT REGION(19,2)\|DISSOLVED INORGANIC CARBON(17,24)\|DEPRESSION(17,4)\|3D MODEL(16,4)\|WATER INFILTRATION(16,3)\|ROTARY TRANSFORMER(16,1)\|RAINFALL INFILTRATION REPLENISHMENT AREA(15,3)\|STORAGE FUNCTION(15,1)\|FIELD GI ANALYSIS(14,3)\|COLLECTION AREA(13,4)\|HCO(13,4)\|RAINFALL SURFACE RUNOFF(12,6)\|FIELD GI(12,3)\|RAINFALL INFILTRATION CHANNEL(12,1)\|RAINFALL INFILTRATION PASSAGE(12,1)\|ADSORPTION PERFORMANCE(10,3)\|RAINFALL INFILTRATION CAPACITY(10,2)\|ECONOMIC PROSPECT(10,1)\|ATMOSPHERIC ABATEMENT(9,1)\|CREATIVE EFFORT(9,1)\|ADSORPTION CAPACITY(8,2)\|CARBON NEUTRALIZATION(8,2)\|DIAMETER FUNCTION(7,4)\|POROSITY(7,3)\|COLLECTION REGION(6,2)\|PERMEABILITY(6,2)\|RETENTION PERFORMANCE(6,2)\|SPRAYING MODE(6,2)\|STAINLESS STEEL ROD(6,2)\|\|(CN114522512)\|CARBON SINK(100,30)\|AQUATIC PHOTOSYNTHESIS(100,12)\|AQUATIC CARBON SINK(100,5)\|AQUATIC ANIMAL(100,2)\|CARBON SINK CAPACITY(100,2)\|DIC FERTILIZATION(69,1)\|AQUATIC CARBON SEQUESTRATION(61,1)\|ATMOSPHERIC CO2IN(51,1)\|AQUATIC CARBON(50,4)\|RAINWATER(49,13)\|GASEOUS FORM2IS(44,3)\|CARBON CIRCULATION(42,1)\|RAIN WATER GUIDE(41,1)\|INORGANIC CARBON(40,11)\|LAND CARBONATE(40,6)\|LAND CARBONATE WEATHERING(38,3)\|SOIL2STORAGE CAPACITY(38,3)\|POPULARIZATION(37,1)\|RAINFALL(35,13)\|SOIL2ENRICHING(35,4)\|RAINFALL INFILTRATION(33,6)\|FIELD2THE PEAT SOIL(32,3)\|AQUATIC PLANT(31,11)\|AQUATIC(29,3)\|ATMOSPHERIC RAINFALL(28,3)\|SOIL PORE(27,8)\|RAINFALL AREA(27,3)\|CARBON SEQUESTRATION(26,5)\|DISSOLVED INORGANIC CARBON(25,25)\|GROUNDWATER(25,9)\|SINK(25,4)\|TERM SCHEMATIC REPRESENTATION(25,1)\|ATMOSPHERE2WITHOUT(23,2)\|NATURAL CONDITION(23,1)\|STABLE ORGANIC CARBON SINK(21,1)\|GROUND LAYER(20,6)\|CARBON SINK SIGNIFICANCE(20,2)\|AQUATIC PHOTOSYNTHETIC ORGANISM PRODUCTIVITY(17,1)\|ORGANIC CARBON SINK(16,2)\|UNDERGROUND WATER(15,4)\|WATERTHE BIOMASS DIC(15,1)\|DREDGE(14,3)\|INORGANIC CARBON VOLUME(14,3)\|PASSAGEWAY(14,3)\|POROSITY(14,3)\|LAYING(14,1)\|ORGANIC CARBON(13,11)\|CARBON SINK FORMATION(13,2)\|WATER BODY(10,20)\|HCO(10,5)\|ATMOSPHERIC CO2THE PATHWAY(10,1)\|UNCHANGING RAINFALL CONDITION PREMISE(10,1)\|PHYTOPLANKTON PRODUCTIVITY(9,1)\|DISSOLVED INORGANIC CARBON CONTENT(8,2)\|DISSOLVED INORGANIC CARBON SOURCE(7,5)\|SURFACE RUNOFF(7,4)\|ATMOSPHERIC CO2STORED(7,1)\|LAND AQUATIC ECOSYSTEM(7,1)\|ATMOSPHERIC CO2AND(6,1)\|CARBON SINK ECONOMIC PROSPECT(6,1)\|CARBONATE WEATHERING CARBON(6,1)\|CREATIVE EFFORT(6,1)\|NATIONAL CARBURANT(6,1)\|RAW MATERIAL(6,1)\|CARBONATE ROCK CONTENT(5,1)\|CO2THE KEY(5,1)\|DIC PROMINENT SOURCE(5,1)\|UNDERGROUND ENVIRONMENT(5,1)\|SURFACE WATER(4,20)\|STEP THREE(4,3)\|PEAT SOIL(4,2)\|CARBON NEUTRALIZATION(4,1)\|CO2THEREFORE(4,1)\|FUNDAMENTAL KEY(4,1)\|LIGHT PARTICIPATION(4,1)\|PHOTOSYNTHESIS2WITH(4,1)\|ALKALINITY(3,1)\|	(CN115445393)\|1. A method for improving the carbon sink efficiency of soil and underground water is characterized by comprising the following steps: the method comprises the following steps:\| Firstly, judging and extracting a main rainfall infiltration supplementing area through site GIS analysis and a DEM three-dimensional model to serve as an area for increasing rainfall infiltration; \| secondly, spreading peat soil with high adsorptivity and high water content to the area selected in the first step, and wetting the dried peat soil with water before spreading; \| thirdly, inserting holes in the peat soil which is well paved, enhancing the permeability of the paved area, and enabling more surface rainfall to enter soil and groundwater space through infiltration so as to increase the CO 2 absorbed by the peat soil; \| And fourthly, increasing the water infiltration amount by adopting a manual sprinkling or leaching mode in a rainfall-free season, increasing the CO 2 amount adsorbed by peat soil, and absorbing and storing atmospheric CO 2 in soil and underground water to form dissolved inorganic carbon so as to realize the purpose of carbon sink. \|2. A method for enhancing the efficiency of carbon sequestration of soil and groundwater according to claim 1, wherein the primary rainfall infiltration replenishment zone in the first step is designated as a rainfall surface runoff collection zone comprising gullies and depressions created by rainfall.\|3. The method for improving the carbon sequestration efficiency of soil and groundwater according to claim 1, wherein the step of spreading peat soil in the second step comprises the steps of: the peat soil with high adsorptivity and high water content is paved in the area selected in the first step, the paving thickness is 5-10cm, the dried peat soil is wetted by water before paving, and the water content of the wetted peat soil is ensured to be 45% -55%.\|4. The method for improving the carbon sequestration efficiency of soil and groundwater according to claim 1, wherein the third step of inserting holes in the tiled peat soil comprises the following steps: the vertical sticks with the diameter of 1cm and the length of 100cm are inserted into the well-paved peat soil, and the density of the formed insertion holes is 10cm multiplied by 10cm, so that more surface rainfall can enter the soil and the groundwater space through infiltration, and the CO 2 absorbed by the peat soil is increased.\|5. The method of claim 1, wherein the dissolved inorganic carbon comprises dissolved CO 2、HCO3- ions and CO 32- ions.	(CN115445393)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of increasing carbon sink and improving carbon circulation, and particularly relates to a method for improving carbon sink efficiency of soil and underground water.\|BACKGROUND ART\|[0002] The aim of China is to realize the aims of carbon reaching peak and carbon neutralization in 2030 and 2060 respectively, and increasing the carbon yield and reducing the carbon emission are the most urgent means for realizing the two aims. However, under the current international economic pressure, the promotion of emission reduction work has certain difficulty in order to ensure good development of economy. Thus, adding carbon sinks or finding new ways of carbon sinks is an important ring to achieve both goals. Carbon sequestration is a mechanism for removing CO 2 from the atmosphere, i.e., absorbing CO 2 from the atmosphere into ecosystems such as land and sea and storing it. Wherein, the soil and the groundwater can form the atmospheric CO 2 into dissolved inorganic carbon (mainly comprising several forms, namely dissolved CO 2(aq)、HCO3- ions and CO 32- ions) through the karst action of rock and the hydrolytic action of CO 2 and water. The part of the formed dissolved inorganic carbon mainly enters soil and underground space through a rainfall infiltration channel under the action of rainfall infiltration flushing and is stored to form a carbon sink process for reducing atmospheric CO 2. In this process, two steps are particularly important, namely, the absorption of CO 2 by the soil, and the surface soil has larger pores and can absorb and store atmospheric CO 2. But the soil has different properties, and the porosity and the adsorption capacity are different; secondly, if CO 2 adsorbed and stored by soil does not enter the deep underground space or enters the dynamic underground water space in time, the CO 2 returns to the atmosphere again, carbon sinks cannot be formed, and the main driving force of the process is leaching effect of rainfall infiltration, namely the amount of the rainfall infiltration into the underground water needs to be increased, so that the amount of the CO 2 entering the deep underground space can be increased more, and more carbon sinks are formed.\|[0003] Therefore, the method for improving the carbon sink efficiency of the soil and the underground water is developed to perfect the engineering technology of carbon sink improvement in China and improve the practical application prospect of the carbon sink.\|DISCLOSURE\|Disclosure of Invention\|[0004] The invention aims to provide a technology for improving carbon sink efficiency of soil and underground water, which is used for improving the carbon sink efficiency of the soil and the underground water for absorbing and storing CO 2 by improving the performance of the soil for absorbing CO 2 and according to the combination form of CO 2 and water in the surface process and the flow circulation mode, and solving the problems in the background technology.\|[0005] In order to solve the technical problems, the invention is realized by the following technical scheme:\|[0006] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps: \|[0007] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; \|[0008] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 45% -55%; \|[0009] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; \|[0010] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. \|[0011] Preferably, the main rainfall infiltration replenishment area in the first step is used as a rainfall surface runoff collection area, and the rainfall surface runoff collection area comprises a gully and a depression formed by rainfall.\|[0012] Preferably, the step of spreading peat soil in the second step specifically includes the following steps: the peat soil with high adsorptivity and high water content is paved in the area selected in the first step, the paving thickness is 5-10cm, the dried peat soil is wetted by water before paving, and the water content of the wetted peat soil is ensured to be 45% -55%.\|[0013] Preferably, the inserting holes on the tiled peat soil in the third step specifically include the following steps: the vertical sticks with the diameter of 1cm and the length of 100cm are inserted into the well-paved peat soil, and the density of the formed insertion holes is 10cm multiplied by 10cm, so that more surface rainfall can enter the soil and the groundwater space through infiltration, and the CO 2 absorbed by the peat soil is increased.\|[0014] Preferably, the dissolved inorganic carbon comprises dissolved CO 2、HCO3- ions and CO 32- ions.\|[0015] Preferably, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other of which is atmospheric CO 2 absorbed by the soil.\|[0016] The invention has the following beneficial effects:\|[0017] According to the invention, the content of dissolved inorganic carbon entering the soil and underground water can be greatly increased through the carrying process of soil adsorption and rainfall infiltration leaching, so that atmospheric CO 2 is stored in a deep underground space, the carbon sink efficiency of the soil and underground water is improved, the method has important carbon sink significance, the efficient removal of CO 2 in the atmosphere can be realized, and the environmental negative effect can not be generated. \|[0018] Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.\|INVENTION MODE\|Detailed Description\|[0019] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.\|[0020] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps:\|[0021] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; \|[0022] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 50%; \|[0023] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; \|[0024] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. \|[0025] According to statistical analysis, the higher the adsorption performance of the soil is, the stronger the adsorption capacity of the soil to atmospheric CO 2 is; in addition, the more rainfall infiltration channels of the soil are, the stronger the rainfall infiltration capacity is, and the more CO 2 is carried by rainfall infiltration, so that the content of dissolved inorganic carbon entering a water body can be effectively increased by 2-3 times by a method of increasing the adsorption quantity of CO 2 in the soil and the rainfall infiltration quantity, and the formed carbon sink quantity is increased by 2-3 times, thereby having important carbon sink economic prospects.\|[0026] In this example, the Dissolved Inorganic Carbon (DIC) includes dissolved CO 2、HCO3- ions and CO 32- ions.\|[0027] In this embodiment, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other is atmospheric CO 2 absorbed by the soil.\|[0028] Increasing the dissolution into the soil and the groundwater is fundamental key to increasing carbon sequestration. While there are two sources of Dissolved Inorganic Carbon (DIC) in soil and groundwater, the highly adsorptive absorption of atmospheric CO 2 by peat soil and the infiltration leaching of atmospheric rainfall carry the absorbed dissolved inorganic carbon. The two parts realize the purposes of reducing, transferring and finally storing the atmospheric CO 2 from the atmosphere into soil and underground water, are the most main CO 2 carbon sink mode, achieve the purpose of increasing carbon sink, and provide technological support for national carburetion sink and realizing important targets of carbon peak and carbon neutralization.\|[0029] In the description of the present specification, the descriptions of the terms "one embodiment," "example," "specific example," and the like, mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.\|[0030] The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof.	(CN115445393)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of increasing carbon sink and improving carbon circulation, and particularly relates to a method for improving carbon sink efficiency of soil and underground water.\|BACKGROUND ART\|[0002] The aim of China is to realize the aims of carbon reaching peak and carbon neutralization in 2030 and 2060 respectively, and increasing the carbon yield and reducing the carbon emission are the most urgent means for realizing the two aims. However, under the current international economic pressure, the promotion of emission reduction work has certain difficulty in order to ensure good development of economy. Thus, adding carbon sinks or finding new ways of carbon sinks is an important ring to achieve both goals. Carbon sequestration is a mechanism for removing CO 2 from the atmosphere, i.e., absorbing CO 2 from the atmosphere into ecosystems such as land and sea and storing it. Wherein, the soil and the groundwater can form the atmospheric CO 2 into dissolved inorganic carbon (mainly comprising several forms, namely dissolved CO 2(aq)、HCO3- ions and CO 32- ions) through the karst action of rock and the hydrolytic action of CO 2 and water. The part of the formed dissolved inorganic carbon mainly enters soil and underground space through a rainfall infiltration channel under the action of rainfall infiltration flushing and is stored to form a carbon sink process for reducing atmospheric CO 2. In this process, two steps are particularly important, namely, the absorption of CO 2 by the soil, and the surface soil has larger pores and can absorb and store atmospheric CO 2. But the soil has different properties, and the porosity and the adsorption capacity are different; secondly, if CO 2 adsorbed and stored by soil does not enter the deep underground space or enters the dynamic underground water space in time, the CO 2 returns to the atmosphere again, carbon sinks cannot be formed, and the main driving force of the process is leaching effect of rainfall infiltration, namely the amount of the rainfall infiltration into the underground water needs to be increased, so that the amount of the CO 2 entering the deep underground space can be increased more, and more carbon sinks are formed.\|[0003] Therefore, the method for improving the carbon sink efficiency of the soil and the underground water is developed to perfect the engineering technology of carbon sink improvement in China and improve the practical application prospect of the carbon sink.\|DISCLOSURE\|Disclosure of Invention\|[0004] The invention aims to provide a technology for improving carbon sink efficiency of soil and underground water, which is used for improving the carbon sink efficiency of the soil and the underground water for absorbing and storing CO 2 by improving the performance of the soil for absorbing CO 2 and according to the combination form of CO 2 and water in the surface process and the flow circulation mode, and solving the problems in the background technology.\|[0005] In order to solve the technical problems, the invention is realized by the following technical scheme:\|[0006] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps: \|[0007] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; \|[0008] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 45% -55%; \|[0009] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; \|[0010] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. \|[0011] Preferably, the main rainfall infiltration replenishment area in the first step is used as a rainfall surface runoff collection area, and the rainfall surface runoff collection area comprises a gully and a depression formed by rainfall.\|[0012] Preferably, the step of spreading peat soil in the second step specifically includes the following steps: the peat soil with high adsorptivity and high water content is paved in the area selected in the first step, the paving thickness is 5-10cm, the dried peat soil is wetted by water before paving, and the water content of the wetted peat soil is ensured to be 45% -55%.\|[0013] Preferably, the inserting holes on the tiled peat soil in the third step specifically include the following steps: the vertical sticks with the diameter of 1cm and the length of 100cm are inserted into the well-paved peat soil, and the density of the formed insertion holes is 10cm multiplied by 10cm, so that more surface rainfall can enter the soil and the groundwater space through infiltration, and the CO 2 absorbed by the peat soil is increased.\|[0014] Preferably, the dissolved inorganic carbon comprises dissolved CO 2、HCO3- ions and CO 32- ions.\|[0015] Preferably, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other of which is atmospheric CO 2 absorbed by the soil.\|[0016] The invention has the following beneficial effects:\|[0017] According to the invention, the content of dissolved inorganic carbon entering the soil and underground water can be greatly increased through the carrying process of soil adsorption and rainfall infiltration leaching, so that atmospheric CO 2 is stored in a deep underground space, the carbon sink efficiency of the soil and underground water is improved, the method has important carbon sink significance, the efficient removal of CO 2 in the atmosphere can be realized, and the environmental negative effect can not be generated. \|[0018] Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.\|INVENTION MODE\|Detailed Description\|[0019] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.\|[0020] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps:\|[0021] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; \|[0022] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 50%; \|[0023] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; \|[0024] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. \|[0025] According to statistical analysis, the higher the adsorption performance of the soil is, the stronger the adsorption capacity of the soil to atmospheric CO 2 is; in addition, the more rainfall infiltration channels of the soil are, the stronger the rainfall infiltration capacity is, and the more CO 2 is carried by rainfall infiltration, so that the content of dissolved inorganic carbon entering a water body can be effectively increased by 2-3 times by a method of increasing the adsorption quantity of CO 2 in the soil and the rainfall infiltration quantity, and the formed carbon sink quantity is increased by 2-3 times, thereby having important carbon sink economic prospects.\|[0026] In this example, the Dissolved Inorganic Carbon (DIC) includes dissolved CO 2、HCO3- ions and CO 32- ions.\|[0027] In this embodiment, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other is atmospheric CO 2 absorbed by the soil.\|[0028] Increasing the dissolution into the soil and the groundwater is fundamental key to increasing carbon sequestration. While there are two sources of Dissolved Inorganic Carbon (DIC) in soil and groundwater, the highly adsorptive absorption of atmospheric CO 2 by peat soil and the infiltration leaching of atmospheric rainfall carry the absorbed dissolved inorganic carbon. The two parts realize the purposes of reducing, transferring and finally storing the atmospheric CO 2 from the atmosphere into soil and underground water, are the most main CO 2 carbon sink mode, achieve the purpose of increasing carbon sink, and provide technological support for national carburetion sink and realizing important targets of carbon peak and carbon neutralization.\|[0029] In the description of the present specification, the descriptions of the terms "one embodiment," "example," "specific example," and the like, mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.\|[0030] The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof.	Family Number\|(100174807)\|100174807\|Object of Invention\|(CN114522512 A)\|The invention discloses a method for increasing aquatic carbon sequestration , and relates to the technical field of carbon sequestration increasing and carbon circulation improving . \|(CN115445393 A)\|( . . . ) circulation mode of the system and water in the earth surface process realize the increase of the absorption and storage of CO in soil and underground water by improving the rainfall infiltration performance of an earth surface system 2 The carbon sequestration efficiency of ( 2 ) solves the problems in the background art . \|The invention discloses a method for improving carbon sequestration efficiency of soil and underground water , and relates to the technical field of carbon sequestration increasing and carbon recycling improving . \|Abstract\|(CN114522512 A)\|The invention discloses a method for increasing the carbon sink amount of aquatic products , and relates to the technical field of carbon sink increasing and carbon cycle improving . The method comprises the following steps : step 1, absorbing atmospheric CO2 in a carbonate rock weathering process , so that CO2 is temporarily captured and stored in soil pores , and enrichment of CO2 in soil is realized ; step 2, by guiding rainwater in the field area during rainfall , rainwater carrying dissolved inorganic carbon is increased to infiltrate into underground water and flows into a surface water body through surface runoff , and the amount of the dissolved inorganic carbon in the surface water body is increased ; and 3, converting dissolved inorganic carbon in the water body into organic carbon through photosynthesis of the aquatic plants , and storing the organic carbon , so that the aquatic carbon sink in the water body is realized . According to the method , the content of dissolved inorganic carbon entering a surface water body can be greatly increased , so that the fertilization effect is improved , the amount of carbon sink formed by aquatic photosynthesis is increased , the method has important carbon sink significance , CO2 in the atmosphere can be efficiently removed , and the environmental negative effect cannot be generated . \|(CN115445393B B)\|The invention discloses a method for improving the carbon sink efficiency of soil and underground water , and relates to the technical field of carbon sink increase and carbon cycle improvement . The method comprises the following steps : step 1, judging and extracting a main rainfall infiltration supply area through site GIS analysis and DEM three - dimensional model , and taking the main rainfall infiltration supply area as an area for increasing the rainfall infiltration amount ; step 2, paving peat soil with a high - adsorbability and high - water - content space to the area selected in the step 1, and wetting the dried peat soil with water before paving ; thirdly , holes are formed in the laid peat soil , the permeability of a laid area is enhanced , more earth surface rainfall can enter the soil and underground water space through infiltration , and the CO2 amount adsorbed by the peat soil is increased . Through soil adsorption and rainfall infiltration leaching carrying processes , the content of dissolved inorganic carbon entering the soil and underground water is greatly increased , so that atmospheric CO2 is stored in a deep underground space , the carbon sequestration efficiency of the soil and underground water is improved , and important carbon sequestration significance is achieved . \|Independent Claims\|(CN114522512 A)\|( . . . ) step two , controlling the rainfall infiltration process : in the first step , inorganic carbon captured and stored in soil pores is mixed with rainwater in the rainfall process to form dissolved inorganic carbon , rainwater carrying the dissolved inorganic carbon is increased to infiltrate into underground water through guiding the rainwater in ( . . . ) \|(CN115445393 A)\|1. A method for improving carbon sequestration efficiency of soil and underground water is characterized by comprising the following steps : the method comprises the following steps : ( . . . ) \|	Environmental technology	B01D-053/14/75\|C02F-003/32\|C02F-2101/10\|C02F-2103/001\|Y02P-060/20		B01D-053/14/75\|C02F-003/32\|C02F-2101/10\|C02F-2103/001\|Y02P-060/20	B01D-053/14\|C02F-003/32	B01D-053/14\|C02F-003/32			CN119028214\|CN117069270	CN119028214 112341928 WHO=Examiner SELF=N CAT=A\|CN117069270 107332388 WHO=Examiner SELF=N CAT=A	AU2020202329\|CN106577116\|CN105130001\|CN102577688	AU2020202329 91096696 WHO=Examiner SELF=N\|CN106577116 75959932 WHO=Examiner SELF=N\|CN105130001 71632395 WHO=Examiner SELF=N\|CN102577688 7762768 WHO=Examiner SELF=N		AU2020202329; CN102577688; CN105130001; CN106577116\|		GRANTED	(CN115445393)\|GRANTED\|(CN114522512)\|LAPSED	ALIVE	(CN115445393)\|ALIVE\|(CN114522512)\|DEAD	(CN115445393)\|LEGAL DETAILS FOR CN115445393\|Actual or expected expiration date=2042-10-26\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2022-10-26\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202211317927\|Application date=2022-10-26\|Standardized application number=2022CN-1317927\|Event publication date=2022-12-09\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN115445393\|Publication stage code=A\|Publication date=2022-12-09\|Standardized publication number=CN115445393\|Event publication date=2022-12-09\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2022-12-27\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2024-04-26\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN115445393\|Publication stage code=B\|Publication date=2024-04-26\|Standardized publication number=CN115445393B\|Event publication date=2024-04-26\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|(CN114522512)\|LEGAL DETAILS FOR CN114522512\|Actual or expected expiration date=2022-12-06\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-01-21\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202210073314\|Application date=2022-01-21\|Standardized application number=2022CN-0073314\|Event publication date=2022-05-24\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN114522512\|Publication stage code=A\|Publication date=2022-05-24\|Standardized publication number=CN114522512\|Event publication date=2022-05-24\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2022-06-10\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2022-12-06\|Event code=CN/WD01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent application deemed withdrawn after publication		(CN115445393)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTeP+miV6FakRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1		https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=KsolU%252FVsjE2he6%252Fe1BZ8qLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN115445393)\|CN\|(CN115445393)\|CN\|(CN114522512)\|CN	(CN115445393)\|NAME=GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY , COUNTRY=CN\|(CN115445393)\|NAME=GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY , COUNTRY=CN\|(CN114522512)\|NAME=GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY , COUNTRY=CN		(CN115445393)\|NAME=CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP) , REG=11308\|(CN115445393)\|NAME=CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP) , REG=11308\|(CN114522512)\|NAME=CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP) , REG=11308	\|(CN115445393)\|CN\|(CN114522512)\|CN	(CN115445393)\|NAME=YANG MINGXING\|NAME=ZHANG MIN\|NAME=YANG WU\|NAME=XIE FEI\|NAME=YAO DUNTING\|NAME=LI WEI\|(CN115445393)\|NAME=YANG MINGXING, COUNTRY=CN \|NAME=ZHANG MIN\|NAME=YANG WU\|NAME=XIE FEI\|NAME=YAO DUNTING\|NAME=LI WEI\|(CN114522512)\|NAME=YANG MINGXING, COUNTRY=CN \|NAME=ZHANG MIN\|NAME=YANG WU\|NAME=XIE FEI		1	2					(CN115445393)\|Number of Claims: NCL=5\|Gazette date: GAZDATE=2024-04-26\|Gazette number: GAZNUM=40-1702\|Number of Pages: NPAGES=5\|Primary examiner: 孙黎\|Primary examiner: Sun Li\|\|(CN115445393)\|Number of Claims: NCL=6\|Gazette date: GAZDATE=2022-12-09\|Gazette number: GAZNUM=38-4902\|Substantial examination effective date: 20221227 Examination duration: 15 months\|Number of Pages: NPAGES=5\|Primary examiner: 孙黎\|Primary examiner: Sun Li\|\|(CN114522512)\|Number of Claims: NCL=5\|Gazette date: GAZDATE=2022-05-24\|Gazette number: GAZNUM=38-2101\|Substantial examination effective date: 20220610\|Number of Pages: NPAGES=5\|	(CN115445393)\|Previous publication: CN115445393 A 2022-12-09 [CN115445393]	(CN115445393)\|CHINESE (CHI)	(CN115445393B)\|Patent\|(CN115445393)\|Patent\|(CN114522512)\|Patent	Titre: (CN115445393)\|Method for improving carbon sink efficiency of soil and underground water Résumé: (CN115445393)\|The invention discloses a method for improving the carbon sink efficiency of soil and underground water, and relates to the technical field of carbon sink increase and carbon cycle improvement. The method comprises the following steps: step 1, judging and extracting a main rainfall infiltration supply area through site GIS analysis and DEM three-dimensional model, and taking the main rainfall infiltration supply area as an area for increasing the rainfall infiltration amount; step 2, paving peat soil with a high-adsorbability and high-water-content space to the area selected in the step 1, and wetting the dried peat soil with water before paving; thirdly, holes are formed in the laid peat soil, the permeability of a laid area is enhanced, more earth surface rainfall can enter the soil and underground water space through infiltration, and the CO2 amount adsorbed by the peat soil is increased. Through soil adsorption and rainfall infiltration leaching carrying processes, the content of dissolved inorganic carbon entering the soil and underground water is greatly increased, so that atmospheric CO2 is stored in a deep underground space, the carbon sequestration efficiency of the soil and underground water is improved, and important carbon sequestration significance is achieved.	20	Abstract	gpt-4o-mini	no	The method focuses on improving carbon sink efficiency through soil and water management rather than accelerating mineral weathering or CO2 capture via mineral carbonation.
22	GB201306559\|GB201406520\|WOEP2015/025018	WOEP2015/025018\|EP15723131\|ES15723131T\|DK15723131T\|CN201580030663\|US15/303,208\|GB201406520\|GB201306559	ES2824676\|DK3129125\|EP3129125\|CN106573197\|US9963351\|CN106573197\|EP3129125\|US20170029284\|GB2516141\|WO2015/154887\|GB2515995\|GB2516141\|GB201406520\|GB201306559	45351908	WO2015/154887 A1 2015-10-15 [WO2015154887]\|EP3129125 B1 2020-07-15 [EP3129125]\|EP3129125 A1 2017-02-15 [EP3129125]\|ES2824676 T3 2021-05-13 [ES2824676]\|DK3129125 T3 2020-10-19 [DK3129125T]\|CN106573197 B 2019-08-23 [CN106573197B]\|CN106573197 A 2017-04-19 [CN106573197]\|US9963351 B2 2018-05-08 [US9963351]\|US20170029284 A1 2017-02-02 [US20170029284]\|GB2516141 B 2016-10-05 [GB2516141]\|GB2516141 A 2015-01-14 [GB2516141]\|GB201406520 D0 2014-05-28 [GB201406520]\|GB2515995 A 2015-01-14 [GB2515995]\|GB201306559 D0 2013-05-22 [GB201306559]	2013-04-10\|2014-04-10\|2015-04-10	2015-04-10\|2015-04-10\|2015-04-10\|2015-04-10\|2015-04-10\|2015-04-10\|2014-04-10\|2013-04-10	2021-05-13\|2020-10-19\|2020-07-15\|2019-08-23\|2018-05-08\|2017-04-19\|2017-02-15\|2017-02-02\|2016-10-05\|2015-10-15\|2015-01-14\|2015-01-14\|2014-05-28\|2013-05-22	(EP3129125)\|2020-07-15\|(US9963351)\|2018-05-08\|\|(GB2516141)\|2016-10-05\|\|(CN106573197B)\|2019-08-23\|(ES2824676)\|2021-05-13\|(DK3129125T)\|2020-10-19	(EP3129125)\|2035-04-10\|(US9963351)\|2035-07-11\|(WO2015/154887)\|2017-10-10\|(GB2516141)\|2024-04-10\|(GB2515995)\|2018-02-21\|(CN106573197)\|2035-04-10\|(ES2824676)\|2035-04-10\|(DK3129125)\|2024-04-30	(EP3129125)\|Method of activation of mineral silicate minerals	(EP3129125)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.	CAMBRIDGE CARBON CAPTURE	(EP3129125)\|Cambridge Carbon Capture Ltd. ([GB])\|(EP3129125)\|Cambridge Carbon Capture Ltd. ([GB])\|(US9963351)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(US20170029284)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(WO2015/154887)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(GB2516141)\|Cambridge Carbon Capture Ltd\|(GB2516141)\|CAMBRIDGE CARBON CAPTURE LTD\|(GB201406520)\|CAMBRIDGE CARBON CAPTURE LTD\|(GB2515995)\|CAMBRIDGE CARBON CAPTURE LTD\|(GB201306559)\|CAMBRIDGE CARBON CAPTURE LTD\|(CN106573197)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(CN106573197)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(ES2824676)\|Cambridge Carbon Capture Ltd.\|(DK3129125)\|Cambridge Carbon Capture Ltd.	PRIESTNALL MICHAEL	(EP3129125)\|PRIESTNALL, Michael\|(EP3129125)\|PRIESTNALL, Michael	(EP3129125)\|Norris, Timothy Sweyn;Basck ([GB])\|Reg. Nb: 101324986\|(WO2015/154887)\|NORRIS, Timothy Sweyn ([GB])\|(CN106573197)\|ZHU HAIYAN;TAHOTA LAW FIRM\|Reg. Nb: 51219	(EP3129125)\|Additional aspects, advantages, features and objects of the present invention would be made apparent from the drawings and the detailed description of the illustrative embodiments construed in conjunction with the appended claims that follow. It will be appreciated that features of the present invention are susceptible to being combined in various combinations from different embodiments without departing from the scope of the present invention as defined by the appended claims.\|From the graph, it will be appreciated that the proportion of Dunite, namely magnesium silicate, converted to Brucite, namely magnesium hydroxide, increases approximately linearly with increase in NaOH concentration; extrapolation of this graph indicates that the proportion of Brucite in the solid product should approach 100% above a NaOH concentration >70mol/kg, namely equivalent to a NaOH: H2O ratio >1.26; FIG. 6 is an illustration of XRD patterns of solid products from dissolution of Dunite at 180 °C with Sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg solution, for different temporal durations; FIG. 7a and 7b are illustrations of TG (7a) and DTG (7b) curves of solid products from dissolution of Dunite at a temperature of 180° C with sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg for different temporal durations; FIG. 8 is a graph in which there is shown Magnesium Hydroxide Mg(OH)2 concentration in solid products based on TG results: Dunite dissolved at a temperature of 180 °C with a molar concentration of Sodium Hydroxide (NaOH) solution being 40 mol/kg for different durations; FIG. 9 is an illustration showing Rietveld Refinement QPA of raw Dunite, wherein: data points profile = experimental pattern; continue profile = calculated model (above); difference plot (below); FIG. 10 is an illustration showing Rietveld Refinement QPA of dissolved Dunite spiked with 10 wt% Silicon, wherein: data points profile = experimental pattern; continue profile = calculated model; and FIG. 11a and 11b are illustrations showing Brucite quantification with Rietveld Refinement and TGA ( FIG. 11a ), wherein Forsterite and Brucite concentrations were obtained via Rietveld Refinement QPA of selected samples ( FIG. 11b ).\|The current invention allows for the method and system to operate without expensive and complicated equipment used in Blencoe to operate at higher than atmospheric pressure.\|Experiments to determine the kinetics of these reactions (5) and (6) have shown that such reactions also suffer from poor energy efficiency and a high cost when up-scaled to an industrial plant.\|However, the efforts suffer from various limitations, such as energy wastage and a high cost of mining and transporting large amounts of rock, as well as industrial and environmental inefficiencies.\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for removal and Capture of Carbon Dioxide from Flue Gases". Although, the prior art disclosures have been able to address some of the problems of mineral Carbonation through their indirect sequestration processes, there are several remaining problems which have not yet been resolved.\|	(EP3129125)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from the group consisting of alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300 °C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|	(EP3129125)\|The present disclosure relates to methods of producing activated mineral silicate for use in sequestrating Carbon Dioxide, for example from flue-gas, by utilizing a process which involves digestion of metal mineral Silicates. Moreover, the present disclosure also relates to systems for executing aforesaid methods.\|The present invention provides a method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, wherein the method comprises: a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from a group comprising alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300°C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|The present invention seeks to provide an improved method of activation of magnesium silicate minerals by conversion to magnesium hydroxide.\|	(EP3129125)\|MAGNESIA(100,30)\|MAGNESIUM SILICATE(100,28)\|MAGNESIUM SILICATE MINERAL(100,12)\|ACTIVATION(100,3)\|MINERAL SILICATE MINERAL ACTIVATION(100,1)\|UNPRESSURIZED VESSEL(84,5)\|BRUCITE QUANTIFICATION(73,1)\|DRY POWDER(67,4)\|RIETVELD REFINEMENT(60,6)\|TEMPORAL DURATION(60,4)\|INEFFICIENCY(60,2)\|MAGNESIUM SILICATE DRY POWDER(60,2)\|BRUCITE PROPORTION(60,1)\|ALKALINE AQUEOUS LIQUID SLURRY(54,2)\|EXPERIMENTAL PATTERN(49,2)\|DISSOLUTION(46,8)\|SHELL INTERNATIONAL(45,1)\|MODEL CALCULATION(42,2)\|MINERAL CARBONATION(41,5)\|MOLAR RATIO(41,4)\|ENERGY WASTAGE(38,1)\|INDIRECT SEQUESTRATION(35,1)\|METAL MINERAL SILICATE DIGESTION(35,1)\|EQUIPMENT COMPLICATION(33,1)\|EXPENSIVE EQUIPMENT(33,1)\|METHANEDIONE(31,30)\|BICARBONATE(31,5)\|DIFFERENCE PLOT(31,1)\|ROCK(31,1)\|XRD PATTERN(30,2)\|ALKALI METAL SILICATE(28,3)\|BRUCITE(27,22)\|MOLAR CONCENTRATION(27,5)\|H2O RATIO(27,1)\|SODIUM HYDROXIDE(26,60)\|AQUEOUS SOLUTION(26,12)\|SOLID PRODUCT(26,8)\|METHANEDIONE SEQUESTRATION(25,5)\|SOLID GLASS PRODUCT(25,4)\|SOLID PRODUCT XRD PATTERN(23,1)\|GLASS PRODUCT(22,4)\|FORSTERITE(22,3)\|METALLIC MINERAL SILICATE(22,1)\|AQUEOUS PHASE PRODUCTION(21,2)\|SEQUESTRATION METHANEDIONE NONINVENTIVE(21,1)\|SODIUM HYDROXIDE MOLAR CONCENTRATION(21,1)\|ALKALI METAL HYDROXIDE(20,7)\|INDUSTRIAL PLANT(20,1)\|MINERAL SILICATE(19,2)\|SODIUM CARBONATE(17,4)\|ALKALI METAL(16,16)\|DTG(16,2)\|SUSPENDED BRUCITE PARTICLE(15,3)\|SEQUESTRATING METHANEDIONE(15,2)\|FORSTERITE CAREFUL QUANTIFICATION(15,1)\|SERPENTINE FEEDSTOCK TONNE(15,1)\|FLUE GAS(14,14)\|ENERGY EFFICIENCY(12,1)\|SALABLE INDUSTRIAL FEEDSTOCK(12,1)\|ATMOSPHERIC PRESSURE(11,8)\|CO2 SCRUBBING(11,2)\|BRUCITE CARBONATION(11,1)\|CONTEMPORARY RESEARCH OVERVIEW(11,1)\|MAGNESIA TONNE(11,1)\|METHANEDIONE TONNE(11,1)\|MINERAL CARBONATION SCIENCE(11,1)\|OLIVINE CARBONATION(11,1)\|DATA POINT PROFILE(10,2)\|DGC REACTOR(10,2)\|BLENCOE ASSERTION(10,1)\|RIETVELD REFINEMENT QPA(10,1)\|SATISFACTORY MINERAL CARBONATION(10,1)\|SERPENTINE DEHYDROXYLATION(10,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(10,1)\|ALKALI METAL COMPOUND(9,9)\|BICARBONATE ION(9,3)\|CO2 REMOVAL(8,4)\|OLIVINE POWDER(8,2)\|ANTHROPOGENIC OXIDATION(8,1)\|CARBONATION REACTOR(8,1)\|INTENSE PREPROCESSING(8,1)\|MAGNESIA DISSOLVE(8,1)\|MAGNESIA POWDER SUSPENSION(8,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(8,1)\|MINERAL CARBONATION REACTION(8,1)\|MINERAL SEQUESTRATION(8,1)\|NONINVENTIVE EXPERIMENT(8,1)\|OLIVINE DIGESTION(8,1)\|SCALABILITY EXPERIMENT(8,1)\|DATA POINT(7,2)\|INORGANIC POWDER(7,2)\|MAGNESIUM SILICATE CONVERSION(7,2)\|MG3SI2O(7,2)\|STEP CONDITION(7,2)\|BRUCITE SOLUBILITY(7,1)\|CARBONACEOUS FOSSIL FUEL(7,1)\|CO2 DISSOLUTION(7,1)\|CO2 TONNE(7,1)\|ELEMENTAL CONSTITUENT(7,1)\|HUGE ENERGY PENALTY(7,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(7,1)\|MASTER THESIS(7,1)\|MINERAL DIGESTION(7,1)\|MINERALOGICAL SITE(7,1)\|MINING HIGH COST(7,1)\|OLIVINE CONVERSION(7,1)\|OVERNIGHT SHUTDOWN(7,1)\|UTILIZATION OPTION(7,1)\|VESSEL PRESSURIZATION(7,1)\|WOLLASTONITE(6,3)\|ROTAMETER(6,2)\|ALKALINE REAGENT(6,1)\|AQUEOUS MAGNESIA(6,1)\|BRUCITE CONVERSION(6,1)\|BRUCITE MINOR PHASE(6,1)\|BRUCITE POWDER(6,1)\|CO2 METER(6,1)\|CO2 TRANSPORT(6,1)\|CYLINDER PREMIX(6,1)\|DIGESTION VESSEL(6,1)\|DUNITE POWDER(6,1)\|INLET CO2(6,1)\|MAGNESIA YIELD(6,1)\|MAGNESIUM ION(6,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(6,1)\|MAGNESIUM SILICATE MINERAL POWDER(6,1)\|METAL SILICATE CARBONATION(6,1)\|MINERAL HYDROXIDE(6,1)\|MOLE RATION(6,1)\|OCCASIONAL MEASUREMENT(6,1)\|PARTICLE ATTRITION(6,1)\|PREMIX CYLINDER(6,1)\|PRESSURIZATION DEPRESSURIZATION(6,1)\|SAMPLE XRD PATTERN(6,1)\|SLURRY CIRCULATION(6,1)\|SLURRY DROPLET SOLUTION(6,1)\|STABLE MINERAL CARBONATE(6,1)\|STOICHIOMETRIC CONVERSION(6,1)\|VALUABLE MINERAL(6,1)\|AMBIENT ATMOSPHERIC PRESSURE(5,4)\|ALKALINE EARTH SILICATE(5,3)\|CAUSTIC ALKALI METAL HYDROXIDE(5,2)\|HIGH COST(5,2)\|MG2SIO(5,2)\|PRODUCTION THROUGHPUT(5,2)\|SEAWATER(5,2)\|ABUNDANT SOURCE(5,1)\|ACIDIC PRETREATMENT(5,1)\|AGEING(5,1)\|ALKALI TREATMENT(5,1)\|ALKALINE PH(5,1)\|AMBIENT ATMOSPHERE(5,1)\|BLEND CONTENT(5,1)\|BRUCITE MAJOR PHASE(5,1)\|BUBBLE COLUMN(5,1)\|CALCIUM SILICATE MINERAL(5,1)\|CALIBRATED GLASS TUBE ROTAMMETER(5,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(5,1)\|CO2 EMISSION DISTANT SOURCE(5,1)\|CO2 SEQUESTRATION CAPACITY(5,1)\|CONTRADISTINCTION(5,1)\|DOMINANT REACTION(5,1)\|DRY STOICHIOMETRIC REACTION(5,1)\|EARTH ATMOSPHERE(5,1)\|ELECTRICITY GENERATING FACILITY(5,1)\|FEED MINERAL(5,1)\|GEOLOGIC TIMESCALE(5,1)\|GLASS SOLIDIFICATION(5,1)\|HUGE SCALE(5,1)\|HYDROTHERMAL REACTION SAVE(5,1)\|INFRARED DATA LOGGER(5,1)\|INLET GAS CO2(5,1)\|INORGANIC PARTICLE(5,1)\|MAGNESIA PRODUCTION(5,1)\|MAGNESIUM BICARBONATE MG(5,1)\|MAGNESIUM SILICATE CRYSTAL(5,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(5,1)\|MAGNESIUM SILICATE PARTICLE(5,1)\|MAGNESIUM SILICATE POWDER(5,1)\|METHANEDIONE SOURCE(5,1)\|MONITORED EXIT GAS(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONEXCLUSIVE(5,1)\|OLIVINE REACTION(5,1)\|PRECAPTURE(5,1)\|PRIMARY INITIATIVE(5,1)\|QUANTITATIVE PHASE ANALYSIS(5,1)\|REACTION ACCELERATOR(5,1)\|RELIANCE(5,1)\|SALABLE CHEMICAL(5,1)\|SEALED VESSEL(5,1)\|SODIUM HYDROXIDE REGENERATION(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|UNPRESSURIZED CONTINUOUS MODE(5,1)\|UNPRESSURIZED REACTION VESSEL(5,1)\|REACTION PRODUCT(4,6)\|HCO(4,3)\|NONUNDERLINED NUMBER(4,3)\|TEMPERATURE ELEVATION(4,3)\|UNDERLINED NUMERAL(4,3)\|2H2O(4,2)\|STOICHIOMETRIC RATIO(3,4)\|ABSOLUTE UNCERTAINTY(3,1)\|ALKALI DIGESTION(3,1)\|ALKALINE COMPOUND INPUT(3,1)\|ALKALINE SOLUTION(3,1)\|ANTIGORITE(3,1)\|AQUEOUS PHASE CARBONATION(3,1)\|AQUEOUS REACTION(3,1)\|AUTOCLAVE(3,1)\|BOUND HYDROXIDE GROUP(3,1)\|CARBONATION DETAIL(3,1)\|CHRYSOTILE(3,1)\|CLEAR BENEFIT(3,1)\|CO2 CONCENTRATION CHANGE(3,1)\|CO2 DEPLETED GAS(3,1)\|CO2 MASS(3,1)\|COMPACTION(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CONCERN CAUSE(3,1)\|CONTAMINATION(3,1)\|DISCOVERY(3,1)\|DISSOLUTION DISINTEGRATION(3,1)\|ECONOMIC FEASIBILITY(3,1)\|EXCESS ALKALI(3,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(3,1)\|\|(EP3129125)\|MAGNESIA(100,30)\|MAGNESIUM SILICATE(100,28)\|MAGNESIUM SILICATE MINERAL(100,12)\|ACTIVATION(100,3)\|MINERAL SILICATE MINERAL ACTIVATION(100,1)\|UNPRESSURIZED VESSEL(84,5)\|BRUCITE QUANTIFICATION(73,1)\|DRY POWDER(67,4)\|RIETVELD REFINEMENT(60,6)\|TEMPORAL DURATION(60,4)\|INEFFICIENCY(60,2)\|MAGNESIUM SILICATE DRY POWDER(60,2)\|BRUCITE PROPORTION(60,1)\|ALKALINE AQUEOUS LIQUID SLURRY(54,2)\|EXPERIMENTAL PATTERN(49,2)\|DISSOLUTION(46,8)\|SHELL INTERNATIONAL(45,1)\|MODEL CALCULATION(42,2)\|MINERAL CARBONATION(41,5)\|MOLAR RATIO(41,4)\|ENERGY WASTAGE(38,1)\|INDIRECT SEQUESTRATION(35,1)\|METAL MINERAL SILICATE DIGESTION(35,1)\|EQUIPMENT COMPLICATION(33,1)\|EXPENSIVE EQUIPMENT(33,1)\|METHANEDIONE(31,30)\|BICARBONATE(31,5)\|DIFFERENCE PLOT(31,1)\|ROCK(31,1)\|XRD PATTERN(30,2)\|ALKALI METAL SILICATE(28,3)\|BRUCITE(27,22)\|MOLAR CONCENTRATION(27,5)\|H2O RATIO(27,1)\|SODIUM HYDROXIDE(26,60)\|AQUEOUS SOLUTION(26,12)\|SOLID PRODUCT(26,8)\|METHANEDIONE SEQUESTRATION(25,5)\|SOLID GLASS PRODUCT(25,4)\|SOLID PRODUCT XRD PATTERN(23,1)\|GLASS PRODUCT(22,4)\|FORSTERITE(22,3)\|METALLIC MINERAL SILICATE(22,1)\|AQUEOUS PHASE PRODUCTION(21,2)\|SEQUESTRATION METHANEDIONE NONINVENTIVE(21,1)\|SODIUM HYDROXIDE MOLAR CONCENTRATION(21,1)\|ALKALI METAL HYDROXIDE(20,7)\|INDUSTRIAL PLANT(20,1)\|MINERAL SILICATE(19,2)\|SODIUM CARBONATE(17,4)\|ALKALI METAL(16,16)\|DTG(16,2)\|SUSPENDED BRUCITE PARTICLE(15,3)\|SEQUESTRATING METHANEDIONE(15,2)\|FORSTERITE CAREFUL QUANTIFICATION(15,1)\|SERPENTINE FEEDSTOCK TONNE(15,1)\|FLUE GAS(14,14)\|ENERGY EFFICIENCY(12,1)\|SALABLE INDUSTRIAL FEEDSTOCK(12,1)\|ATMOSPHERIC PRESSURE(11,8)\|CO2 SCRUBBING(11,2)\|BRUCITE CARBONATION(11,1)\|CONTEMPORARY RESEARCH OVERVIEW(11,1)\|MAGNESIA TONNE(11,1)\|METHANEDIONE TONNE(11,1)\|MINERAL CARBONATION SCIENCE(11,1)\|OLIVINE CARBONATION(11,1)\|DATA POINT PROFILE(10,2)\|DGC REACTOR(10,2)\|BLENCOE ASSERTION(10,1)\|RIETVELD REFINEMENT QPA(10,1)\|SATISFACTORY MINERAL CARBONATION(10,1)\|SERPENTINE DEHYDROXYLATION(10,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(10,1)\|ALKALI METAL COMPOUND(9,9)\|BICARBONATE ION(9,3)\|CO2 REMOVAL(8,4)\|OLIVINE POWDER(8,2)\|ANTHROPOGENIC OXIDATION(8,1)\|CARBONATION REACTOR(8,1)\|INTENSE PREPROCESSING(8,1)\|MAGNESIA DISSOLVE(8,1)\|MAGNESIA POWDER SUSPENSION(8,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(8,1)\|MINERAL CARBONATION REACTION(8,1)\|MINERAL SEQUESTRATION(8,1)\|NONINVENTIVE EXPERIMENT(8,1)\|OLIVINE DIGESTION(8,1)\|SCALABILITY EXPERIMENT(8,1)\|DATA POINT(7,2)\|INORGANIC POWDER(7,2)\|MAGNESIUM SILICATE CONVERSION(7,2)\|MG3SI2O(7,2)\|STEP CONDITION(7,2)\|BRUCITE SOLUBILITY(7,1)\|CARBONACEOUS FOSSIL FUEL(7,1)\|CO2 DISSOLUTION(7,1)\|CO2 TONNE(7,1)\|ELEMENTAL CONSTITUENT(7,1)\|HUGE ENERGY PENALTY(7,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(7,1)\|MASTER THESIS(7,1)\|MINERAL DIGESTION(7,1)\|MINERALOGICAL SITE(7,1)\|MINING HIGH COST(7,1)\|OLIVINE CONVERSION(7,1)\|OVERNIGHT SHUTDOWN(7,1)\|UTILIZATION OPTION(7,1)\|VESSEL PRESSURIZATION(7,1)\|WOLLASTONITE(6,3)\|ROTAMETER(6,2)\|ALKALINE REAGENT(6,1)\|AQUEOUS MAGNESIA(6,1)\|BRUCITE CONVERSION(6,1)\|BRUCITE MINOR PHASE(6,1)\|BRUCITE POWDER(6,1)\|CO2 METER(6,1)\|CO2 TRANSPORT(6,1)\|CYLINDER PREMIX(6,1)\|DIGESTION VESSEL(6,1)\|DUNITE POWDER(6,1)\|INLET CO2(6,1)\|MAGNESIA YIELD(6,1)\|MAGNESIUM ION(6,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(6,1)\|MAGNESIUM SILICATE MINERAL POWDER(6,1)\|METAL SILICATE CARBONATION(6,1)\|MINERAL HYDROXIDE(6,1)\|MOLE RATION(6,1)\|OCCASIONAL MEASUREMENT(6,1)\|PARTICLE ATTRITION(6,1)\|PREMIX CYLINDER(6,1)\|PRESSURIZATION DEPRESSURIZATION(6,1)\|SAMPLE XRD PATTERN(6,1)\|SLURRY CIRCULATION(6,1)\|SLURRY DROPLET SOLUTION(6,1)\|STABLE MINERAL CARBONATE(6,1)\|STOICHIOMETRIC CONVERSION(6,1)\|VALUABLE MINERAL(6,1)\|AMBIENT ATMOSPHERIC PRESSURE(5,4)\|ALKALINE EARTH SILICATE(5,3)\|CAUSTIC ALKALI METAL HYDROXIDE(5,2)\|HIGH COST(5,2)\|MG2SIO(5,2)\|PRODUCTION THROUGHPUT(5,2)\|SEAWATER(5,2)\|ABUNDANT SOURCE(5,1)\|ACIDIC PRETREATMENT(5,1)\|AGEING(5,1)\|ALKALI TREATMENT(5,1)\|ALKALINE PH(5,1)\|AMBIENT ATMOSPHERE(5,1)\|BLEND CONTENT(5,1)\|BRUCITE MAJOR PHASE(5,1)\|BUBBLE COLUMN(5,1)\|CALCIUM SILICATE MINERAL(5,1)\|CALIBRATED GLASS TUBE ROTAMMETER(5,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(5,1)\|CO2 EMISSION DISTANT SOURCE(5,1)\|CO2 SEQUESTRATION CAPACITY(5,1)\|CONTRADISTINCTION(5,1)\|DOMINANT REACTION(5,1)\|DRY STOICHIOMETRIC REACTION(5,1)\|EARTH ATMOSPHERE(5,1)\|ELECTRICITY GENERATING FACILITY(5,1)\|FEED MINERAL(5,1)\|GEOLOGIC TIMESCALE(5,1)\|GLASS SOLIDIFICATION(5,1)\|HUGE SCALE(5,1)\|HYDROTHERMAL REACTION SAVE(5,1)\|INFRARED DATA LOGGER(5,1)\|INLET GAS CO2(5,1)\|INORGANIC PARTICLE(5,1)\|MAGNESIA PRODUCTION(5,1)\|MAGNESIUM BICARBONATE MG(5,1)\|MAGNESIUM SILICATE CRYSTAL(5,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(5,1)\|MAGNESIUM SILICATE PARTICLE(5,1)\|MAGNESIUM SILICATE POWDER(5,1)\|METHANEDIONE SOURCE(5,1)\|MONITORED EXIT GAS(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONEXCLUSIVE(5,1)\|OLIVINE REACTION(5,1)\|PRECAPTURE(5,1)\|PRIMARY INITIATIVE(5,1)\|QUANTITATIVE PHASE ANALYSIS(5,1)\|REACTION ACCELERATOR(5,1)\|RELIANCE(5,1)\|SALABLE CHEMICAL(5,1)\|SEALED VESSEL(5,1)\|SODIUM HYDROXIDE REGENERATION(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|UNPRESSURIZED CONTINUOUS MODE(5,1)\|UNPRESSURIZED REACTION VESSEL(5,1)\|REACTION PRODUCT(4,6)\|HCO(4,3)\|NONUNDERLINED NUMBER(4,3)\|TEMPERATURE ELEVATION(4,3)\|UNDERLINED NUMERAL(4,3)\|2H2O(4,2)\|STOICHIOMETRIC RATIO(3,4)\|ABSOLUTE UNCERTAINTY(3,1)\|ALKALI DIGESTION(3,1)\|ALKALINE COMPOUND INPUT(3,1)\|ALKALINE SOLUTION(3,1)\|ANTIGORITE(3,1)\|AQUEOUS PHASE CARBONATION(3,1)\|AQUEOUS REACTION(3,1)\|AUTOCLAVE(3,1)\|BOUND HYDROXIDE GROUP(3,1)\|CARBONATION DETAIL(3,1)\|CHRYSOTILE(3,1)\|CLEAR BENEFIT(3,1)\|CO2 CONCENTRATION CHANGE(3,1)\|CO2 DEPLETED GAS(3,1)\|CO2 MASS(3,1)\|COMPACTION(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CONCERN CAUSE(3,1)\|CONTAMINATION(3,1)\|DISCOVERY(3,1)\|DISSOLUTION DISINTEGRATION(3,1)\|ECONOMIC FEASIBILITY(3,1)\|EXCESS ALKALI(3,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(3,1)\|\|(US9963351)\|MAGNESIA(100,40)\|MAGNESIUM SILICATE(100,33)\|MAGNESIUM SILICATE MINERAL(100,14)\|ACTIVATION(100,6)\|MINERAL SILICATE MINERAL ACTIVATION(100,1)\|MINERAL CARBONATION(79,6)\|INEFFICIENCY(60,2)\|OLIVINE CONVERSION(60,1)\|UNPRESSURIZED VESSEL(59,6)\|METHANEDIONE SEQUESTRATION(52,6)\|ALKALINE AQUEOUS LIQUID SLURRY(50,4)\|ALKALI DIGESTION(48,1)\|SHELL INTERNATIONAL(45,1)\|SERPENTINE MINERAL(43,1)\|DRY POWDER(41,4)\|OLIVINE ROCK(41,1)\|ENERGY WASTAGE(38,1)\|SODIUM HYDROXIDE REGENERATION(38,1)\|MAGNESIUM SILICATE DRY POWDER(37,2)\|CONTRADISTINCTION(35,1)\|EXPERIMENTAL CONDITION EXPLORATION(35,1)\|INDIRECT SEQUESTRATION(35,1)\|NATURALLY OCCURRING OLIVINE(35,1)\|EQUIPMENT COMPLICATION(33,1)\|EXPENSIVE EQUIPMENT(33,1)\|METHANEDIONE(32,42)\|OLIVINE SODIUM HYDROXIDE REACTION(32,1)\|MAGNESIUM SILICATE ROCK(31,1)\|ROCK(31,1)\|ALKALI METAL SILICATE(29,5)\|AQUEOUS SOLUTION(28,16)\|CARBONATION DETAIL(28,1)\|MOLAR RATIO(27,6)\|ALKALI DIGESTION(27,1)\|BRUCITE(22,22)\|SEQUESTRATION(22,10)\|SEQUESTRATING METHANEDIONE(22,4)\|OPEN VESSEL(21,1)\|AQUEOUS PHASE PRODUCTION(19,4)\|SODIUM CARBONATE(17,4)\|REACTION PRESSURE(17,1)\|SODIUM HYDROXIDE(16,72)\|SOLID GLASS PRODUCT(16,5)\|EXPERIMENTAL CONDITION(16,1)\|GLASS PRODUCT(15,5)\|TEMPERATURE ELEVATION(15,4)\|SUSPENDED BRUCITE PARTICLE(15,3)\|FORSTERITE CAREFUL QUANTIFICATION(15,1)\|SERPENTINE FEEDSTOCK TONNE(15,1)\|ALKALI METAL HYDROXIDE(14,6)\|ALKALI METAL(13,20)\|ATMOSPHERIC PRESSURE(13,10)\|TEMPORAL DURATION(13,4)\|MINERAL FEEDSTOCK CARBONATION(13,1)\|FLUE GAS(12,24)\|SOLID PRODUCT(12,10)\|ALKALINE EARTH SILICATE(12,8)\|AMBIENT ATMOSPHERIC PRESSURE(12,7)\|SALABLE INDUSTRIAL FEEDSTOCK(12,1)\|CO2 SCRUBBING(11,2)\|BRUCITE CARBONATION(11,1)\|CONTEMPORARY RESEARCH OVERVIEW(11,1)\|MAGNESIA CARBONATION(11,1)\|MAGNESIA TONNE(11,1)\|METHANEDIONE TONNE(11,1)\|MINERAL CARBONATION SCIENCE(11,1)\|OLIVINE CARBONATION(11,1)\|SEQUESTRATION METHANEDIONE(11,1)\|UNPRESSURIZED AQUEOUS CARBONATION(11,1)\|DGC REACTOR(10,2)\|BLENCOE ASSERTION(10,1)\|BRUCITE QUANTIFICATION(10,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(10,1)\|RIETVELD REFINEMENT QPA(10,1)\|SATISFACTORY MINERAL CARBONATION(10,1)\|SERPENTINE DEHYDROXYLATION(10,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(10,1)\|BICARBONATE ION(9,3)\|WATER VAPOR PRESSURE(9,3)\|CO2 REMOVAL(8,4)\|MAGNESIUM SILICATE CONVERSION(8,3)\|OLIVINE POWDER(8,2)\|ANTHROPOGENIC OXIDATION(8,1)\|CARBONATION REACTOR(8,1)\|INTENSE PREPROCESSING(8,1)\|MAGNESIA DISSOLVE(8,1)\|MAGNESIA POWDER SUSPENSION(8,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(8,1)\|MINERAL CARBONATION REACTION(8,1)\|MINERAL SEQUESTRATION(8,1)\|OLIVINE DIGESTION(8,1)\|PROPOSED MINERAL CARBONATION(8,1)\|SCALABILITY EXPERIMENT(8,1)\|VAPOR PRESSURE(7,8)\|WOLLASTONITE(7,4)\|BLEND CONTENT(7,2)\|ENERGY EFFICIENCY(7,2)\|EXPERIMENTAL PATTERN(7,2)\|INORGANIC POWDER(7,2)\|METHANEDIONE SOURCE(7,2)\|UNPRESSURIZED CONTINUOUS MODE(7,2)\|BRUCITE DISPERSION(7,1)\|BRUCITE POWDER SEPARATION(7,1)\|BRUCITE PROPORTION(7,1)\|BRUCITE SOLUBILITY(7,1)\|CARBONACEOUS FOSSIL FUEL(7,1)\|CO2 DISSOLUTION(7,1)\|CO2 TONNE(7,1)\|DIRT ATTRITION(7,1)\|ELEMENTAL CONSTITUENT(7,1)\|HUGE ENERGY PENALTY(7,1)\|MAGNESIA INTEREST(7,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(7,1)\|MASTER THESIS(7,1)\|MINERAL DIGESTION(7,1)\|MINERALOGICAL SITE(7,1)\|MINING HIGH COST(7,1)\|OVERNIGHT SHUTDOWN(7,1)\|SILICATE MINERAL CARBONATION(7,1)\|STIRRED TEFLON VESSEL(7,1)\|UTILIZATION OPTION(7,1)\|VESSEL PRESSURIZATION(7,1)\|MG2SIO(6,3)\|EXCESS CONSUMPTION(6,2)\|ROTAMETER(6,2)\|ALKALINE REAGENT(6,1)\|AMBIENT UNPRESSURIZED CONDITION(6,1)\|AQUEOUS MAGNESIA(6,1)\|BRUCITE CONVERSION(6,1)\|BRUCITE MINOR PHASE(6,1)\|CO2 ED(6,1)\|CO2 TRANSPORT(6,1)\|CYLINDER PREMIX(6,1)\|DIGESTION VESSEL(6,1)\|DUNITE POWDER(6,1)\|H2O MOLAR RATIO(6,1)\|INLET CO2(6,1)\|MAGNESIA YIELD(6,1)\|MAGNESIUM ION(6,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(6,1)\|MAGNESIUM SILICATE MINERAL POWDER(6,1)\|METAL SILICATE CARBONATION(6,1)\|MINERAL HYDROXIDE(6,1)\|MOLE RATION(6,1)\|OCCASIONAL MEASUREMENT(6,1)\|PARTICLE ATTRITION(6,1)\|PREMIX CYLINDER(6,1)\|SAMPLE XRD PATTERN(6,1)\|SLURRY CIRCULATION(6,1)\|SLURRY DROPLET SOLUTION(6,1)\|STABLE MINERAL CARBONATE(6,1)\|STOICHIOMETRIC CONVERSION(6,1)\|STOICHIOMETRIC MOLAR RATIO(6,1)\|VALUABLE MINERAL(6,1)\|WATER CARBONATION REACTION(6,1)\|HCO(5,5)\|MGCO(5,4)\|CAUSTIC ALKALI METAL HYDROXIDE(5,2)\|METAL MINERAL SILICATE DIGESTION(5,2)\|MODEL CALCULATION(5,2)\|MOLALITY(5,2)\|PRODUCTION THROUGHPUT(5,2)\|SEAWATER(5,2)\|ABUNDANT SOURCE(5,1)\|ACIDIC PRETREATMENT(5,1)\|AGEING(5,1)\|ALKALI TREATMENT(5,1)\|ALKALINE PH(5,1)\|AMBIENT ATMOSPHERE(5,1)\|BRUCITE MAJOR PHASE(5,1)\|BUBBLE COLUMN(5,1)\|CALCIUM SILICATE MINERAL(5,1)\|CALIBRATED GLASS TUBE ROTAMMETER(5,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(5,1)\|CO2 EMISSION DISTANT SOURCE(5,1)\|CO2 EXPENSIVE SEPARATION(5,1)\|CO2 REACTION(5,1)\|CO2 SEQUESTRATION CAPACITY(5,1)\|DOMINANT REACTION(5,1)\|DRY STOICHIOMETRIC REACTION(5,1)\|EARTH ATMOSPHERE(5,1)\|ELECTRICITY GENERATING FACILITY(5,1)\|FEED MINERAL(5,1)\|GEOLOGIC TIMESCALE(5,1)\|GLASS SOLIDIFICATION(5,1)\|HUGE SCALE(5,1)\|HYDROTHERMAL REACTION SAVE(5,1)\|INFRARED DATA LOGGER(5,1)\|INLET GAS CO2(5,1)\|INORGANIC PARTICLE(5,1)\|MAGNESIA PRODUCTION(5,1)\|MAGNESIA WEIGHT(5,1)\|MAGNESIUM BICARBONATE MG(5,1)\|MAGNESIUM SILICATE CRYSTAL(5,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(5,1)\|MAGNESIUM SILICATE PARTICLE(5,1)\|MAGNESIUM SILICATE POWDER(5,1)\|MONITORED EXIT GAS(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONEXCLUSIVE(5,1)\|OLIVINE REACTION(5,1)\|PRECAPTURE(5,1)\|PRESSURIZATION DEPRESSURIZATION(5,1)\|PRIMARY INITIATIVE(5,1)\|QUANTITATIVE PHASE ANALYSIS(5,1)\|REACTION ACCELERATOR(5,1)\|REACTION SOLUBLE FRACTION(5,1)\|RELIANCE(5,1)\|SALABLE CHEMICAL(5,1)\|SEALED VESSEL(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|UNPRESSURIZED REACTION VESSEL(5,1)\|UNSEPARATED FLUE GAS(5,1)\|REACTION PRODUCT(4,7)\|NONUNDERLINED NUMBER(4,3)\|UNDERLINED NUMERAL(4,3)\|GAS MIXTURE(3,10)\|STOICHIOMETRIC RATIO(3,4)\|ABSOLUTE UNCERTAINTY(3,1)\|ALKALINE COMPOUND INPUT(3,1)\|ALKALINE SOLUTION(3,1)\|AMBIENT PRESSURE CARBONATION(3,1)\|ANTIGORITE(3,1)\|AQUEOUS PHASE CARBONATION(3,1)\|AQUEOUS REACTION(3,1)\|AUTOCLAVE(3,1)\|BLENDING SYSTEM(3,1)\|BOUND HYDROXIDE GROUP(3,1)\|CHRYSOTILE(3,1)\|CLEAR BENEFIT(3,1)\|CO2 CONCENTRATION CHANGE(3,1)\|CO2 DEPLETED GAS(3,1)\|CO2 MASS(3,1)\|COMPACTION(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CONCERN CAUSE(3,1)\|CONSUMPTION CONDITION(3,1)\|CONTAMINATION(3,1)\|DIFFERENCE PLOT(3,1)\|DISCOVERY(3,1)\|DISSOLUTION DISINTEGRATION(3,1)\|ECONOMIC FEASIBILITY(3,1)\|EXCESS ALKALI(3,1)\|\|(US20170029284)\|MAGNESIA(100,40)\|MAGNESIUM SILICATE(100,33)\|MAGNESIUM SILICATE MINERAL(100,14)\|ACTIVATION(100,6)\|MINERAL SILICATE MINERAL ACTIVATION(100,1)\|MINERAL CARBONATION(79,6)\|INEFFICIENCY(60,2)\|OLIVINE CONVERSION(60,1)\|UNPRESSURIZED VESSEL(59,6)\|METHANEDIONE SEQUESTRATION(52,6)\|ALKALI DIGESTION(48,1)\|SHELL INTERNATIONAL(45,1)\|ALKALINE AQUEOUS LIQUID SLURRY(43,3)\|SERPENTINE MINERAL(43,1)\|DRY POWDER(41,4)\|OLIVINE ROCK(41,1)\|ENERGY WASTAGE(38,1)\|SODIUM HYDROXIDE REGENERATION(38,1)\|MAGNESIUM SILICATE DRY POWDER(37,2)\|CONTRADISTINCTION(35,1)\|EXPERIMENTAL CONDITION EXPLORATION(35,1)\|INDIRECT SEQUESTRATION(35,1)\|NATURALLY OCCURRING OLIVINE(35,1)\|EQUIPMENT COMPLICATION(33,1)\|EXPENSIVE EQUIPMENT(33,1)\|METHANEDIONE(32,42)\|OLIVINE SODIUM HYDROXIDE REACTION(32,1)\|MAGNESIUM SILICATE ROCK(31,1)\|ROCK(31,1)\|ALKALI METAL SILICATE(29,5)\|AQUEOUS SOLUTION(28,16)\|CARBONATION DETAIL(28,1)\|MOLAR RATIO(27,6)\|ALKALI DIGESTION(27,1)\|BRUCITE(22,22)\|SEQUESTRATION(22,10)\|SEQUESTRATING METHANEDIONE(22,4)\|OPEN VESSEL(21,1)\|AQUEOUS PHASE PRODUCTION(19,4)\|CO2 SEQUESTRATION(19,2)\|SODIUM CARBONATE(17,4)\|REACTION PRESSURE(17,1)\|SODIUM HYDROXIDE(16,72)\|SOLID GLASS PRODUCT(16,5)\|EXPERIMENTAL CONDITION(16,1)\|GLASS PRODUCT(15,5)\|TEMPERATURE ELEVATION(15,4)\|SUSPENDED BRUCITE PARTICLE(15,3)\|FORSTERITE CAREFUL QUANTIFICATION(15,1)\|SERPENTINE FEEDSTOCK TONNE(15,1)\|ALKALI METAL HYDROXIDE(14,6)\|ALKALI METAL(13,20)\|ATMOSPHERIC PRESSURE(13,10)\|TEMPORAL DURATION(13,4)\|MINERAL FEEDSTOCK CARBONATION(13,1)\|FLUE GAS(12,24)\|SOLID PRODUCT(12,10)\|ALKALINE EARTH SILICATE(12,8)\|AMBIENT ATMOSPHERIC PRESSURE(12,7)\|SALABLE INDUSTRIAL FEEDSTOCK(12,1)\|CO2 SCRUBBING(11,2)\|BRUCITE CARBONATION(11,1)\|CONTEMPORARY RESEARCH OVERVIEW(11,1)\|MAGNESIA CARBONATION(11,1)\|MAGNESIA TONNE(11,1)\|METHANEDIONE TONNE(11,1)\|MINERAL CARBONATION SCIENCE(11,1)\|OLIVINE CARBONATION(11,1)\|SEQUESTRATION METHANEDIONE(11,1)\|UNPRESSURIZED AQUEOUS CARBONATION(11,1)\|DGC REACTOR(10,2)\|BLENCOE ASSERTION(10,1)\|BRUCITE QUANTIFICATION(10,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(10,1)\|RIETVELD REFINEMENT QPA(10,1)\|SATISFACTORY MINERAL CARBONATION(10,1)\|SERPENTINE DEHYDROXYLATION(10,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(10,1)\|BICARBONATE ION(9,3)\|WATER VAPOR PRESSURE(9,3)\|CO2 REMOVAL(8,4)\|MAGNESIUM SILICATE CONVERSION(8,3)\|OLIVINE POWDER(8,2)\|ANTHROPOGENIC OXIDATION(8,1)\|CARBONATION REACTOR(8,1)\|INTENSE PREPROCESSING(8,1)\|MAGNESIA DISSOLVE(8,1)\|MAGNESIA POWDER SUSPENSION(8,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(8,1)\|MINERAL CARBONATION REACTION(8,1)\|MINERAL SEQUESTRATION(8,1)\|OLIVINE DIGESTION(8,1)\|PROPOSED MINERAL CARBONATION(8,1)\|SCALABILITY EXPERIMENT(8,1)\|VAPOR PRESSURE(7,8)\|WOLLASTONITE(7,4)\|BLEND CONTENT(7,2)\|ENERGY EFFICIENCY(7,2)\|EXPERIMENTAL PATTERN(7,2)\|INORGANIC POWDER(7,2)\|METHANEDIONE SOURCE(7,2)\|UNPRESSURIZED CONTINUOUS MODE(7,2)\|BRUCITE DISPERSION(7,1)\|BRUCITE POWDER SEPARATION(7,1)\|BRUCITE PROPORTION(7,1)\|BRUCITE SOLUBILITY(7,1)\|CARBONACEOUS FOSSIL FUEL(7,1)\|CO2 DISSOLUTION(7,1)\|CO2 TONNE(7,1)\|ELEMENTAL CONSTITUENT(7,1)\|HUGE ENERGY PENALTY(7,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(7,1)\|MASTER THESIS(7,1)\|MINERAL DIGESTION(7,1)\|MINERALOGICAL SITE(7,1)\|MINING HIGH COST(7,1)\|OVERNIGHT SHUTDOWN(7,1)\|SILICATE MINERAL CARBONATION(7,1)\|STIRRED TEFLON VESSEL(7,1)\|UTILIZATION OPTION(7,1)\|VESSEL PRESSURIZATION(7,1)\|EXCESS CONSUMPTION(6,2)\|ROTAMETER(6,2)\|ALKALINE REAGENT(6,1)\|AMBIENT UNPRESSURIZED CONDITION(6,1)\|AQUEOUS MAGNESIA(6,1)\|BRUCITE CONVERSION(6,1)\|BRUCITE MINOR PHASE(6,1)\|CO2 METER(6,1)\|CO2 TRANSPORT(6,1)\|COSEQUESTRATION CAPACITY(6,1)\|CYLINDER PREMIX(6,1)\|DIGESTION VESSEL(6,1)\|DUNITE POWDER(6,1)\|H2O MOLAR RATIO(6,1)\|INLET CO2(6,1)\|MAGNESIA FORMATION(6,1)\|MAGNESIA YIELD(6,1)\|MAGNESIUM ION(6,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(6,1)\|MAGNESIUM SILICATE MINERAL POWDER(6,1)\|METAL SILICATE CARBONATION(6,1)\|MINERAL HYDROXIDE(6,1)\|MOLE RATION(6,1)\|OCCASIONAL MEASUREMENT(6,1)\|PARTICLE ATTRITION(6,1)\|PREMIX CYLINDER(6,1)\|SAMPLE XRD PATTERN(6,1)\|SLURRY CIRCULATION(6,1)\|SLURRY DROPLET SOLUTION(6,1)\|STABLE MINERAL CARBONATE(6,1)\|STOICHIOMETRIC CONVERSION(6,1)\|STOICHIOMETRIC MOLAR RATIO(6,1)\|VALUABLE MINERAL(6,1)\|WATER CARBONATION REACTION(6,1)\|HCO(5,4)\|CAUSTIC ALKALI METAL HYDROXIDE(5,2)\|LITER WATER(5,2)\|METAL MINERAL SILICATE DIGESTION(5,2)\|MG2SIO(5,2)\|MODEL CALCULATION(5,2)\|MOLALITY(5,2)\|PRODUCTION THROUGHPUT(5,2)\|SEAWATER(5,2)\|ABUNDANT SOURCE(5,1)\|ACIDIC PRETREATMENT(5,1)\|AGEING(5,1)\|ALKALI TREATMENT(5,1)\|ALKALINE PH(5,1)\|AMBIENT ATMOSPHERE(5,1)\|BRUCITE MAJOR PHASE(5,1)\|BUBBLE COLUMN(5,1)\|CALCIUM SILICATE MINERAL(5,1)\|CALIBRATED GLASS TUBE ROTAMMETER(5,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(5,1)\|CO2 EMISSION DISTANT SOURCE(5,1)\|CO2 EXPENSIVE SEPARATION(5,1)\|CO2 REACTION(5,1)\|DOMINANT REACTION(5,1)\|DRY STOICHIOMETRIC REACTION(5,1)\|EARTH ATMOSPHERE(5,1)\|ELECTRICITY GENERATING FACILITY(5,1)\|FEED MINERAL(5,1)\|GEOLOGIC TIMESCALE(5,1)\|GLASS SOLIDIFICATION(5,1)\|HUGE SCALE(5,1)\|HYDROTHERMAL REACTION SAVE(5,1)\|INFRARED DATA LOGGER(5,1)\|INLET GAS CO2(5,1)\|INORGANIC PARTICLE(5,1)\|MAGNESIA PRODUCTION(5,1)\|MAGNESIA WEIGHT(5,1)\|MAGNESIUM BICARBONATE MG(5,1)\|MAGNESIUM SILICATE CRYSTAL(5,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(5,1)\|MAGNESIUM SILICATE PARTICLE(5,1)\|MAGNESIUM SILICATE POWDER(5,1)\|MONITORED EXIT GAS(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONEXCLUSIVE(5,1)\|OLIVINE REACTION(5,1)\|PRECAPTURE(5,1)\|PRESSURIZATION DEPRESSURIZATION(5,1)\|PRIMARY INITIATIVE(5,1)\|QUANTITATIVE PHASE ANALYSIS(5,1)\|REACTION ACCELERATOR(5,1)\|REACTION SOLUBLE FRACTION(5,1)\|RELIANCE(5,1)\|SALABLE CHEMICAL(5,1)\|SEALED VESSEL(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|UNPRESSURIZED REACTION VESSEL(5,1)\|UNSEPARATED FLUE GAS(5,1)\|REACTION PRODUCT(4,7)\|MGCO(4,3)\|NONUNDERLINED NUMBER(4,3)\|UNDERLINED NUMERAL(4,3)\|GAS MIXTURE(3,10)\|STOICHIOMETRIC RATIO(3,4)\|ABSOLUTE UNCERTAINTY(3,1)\|ALKALINE COMPOUND INPUT(3,1)\|ALKALINE SOLUTION(3,1)\|AMBIENT PRESSURE CARBONATION(3,1)\|ANTIGORITE(3,1)\|AQUEOUS PHASE CARBONATION(3,1)\|AQUEOUS REACTION(3,1)\|AUTOCLAVE(3,1)\|BLENDING SYSTEM(3,1)\|BOUND HYDROXIDE GROUP(3,1)\|CHRYSOTILE(3,1)\|CLEAR BENEFIT(3,1)\|CO2 CONCENTRATION CHANGE(3,1)\|CO2 DEPLETED GAS(3,1)\|CO2 MASS(3,1)\|COMPACTION(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CONCERN CAUSE(3,1)\|CONSUMPTION CONDITION(3,1)\|CONTAMINATION(3,1)\|DIFFERENCE PLOT(3,1)\|\|(WO2015/154887)\|MAGNESIA(100,38)\|MAGNESIUM SILICATE(100,31)\|MAGNESIUM SILICATE MINERAL(100,14)\|UNPRESSURIZED VESSEL(100,6)\|ACTIVATION(100,5)\|DRY POWDER(69,4)\|MAGNESIUM SILICATE DRY POWDER(62,2)\|ALKALINE AQUEOUS LIQUID SLURRY(56,2)\|MOLAR RATIO(46,6)\|METHANEDIONE SEQUESTRATION(43,5)\|BLEND CONTENT(37,2)\|ALKALINE COMPOUND(35,9)\|DISSOLUTION(35,9)\|AQUEOUS SOLUTION(34,14)\|SEQUESTRATING METHANEDIONE(32,3)\|SODIUM CARBONATE(32,3)\|ALKALI METAL SILICATE(30,3)\|SOLID GLASS PRODUCT(25,4)\|SUSPENDED BRUCITE PARTICLE(25,3)\|FORSTERITE CAREFUL QUANTIFICATION(25,1)\|SERPENTINE FEEDSTOCK TONNE(25,1)\|GLASS PRODUCT(23,4)\|TEMPORAL DURATION(23,4)\|REACTION CHAMBER BLENDING CONTENT(23,2)\|MINERAL FEEDSTOCK CARBONATION(23,1)\|SALABLE INDUSTRIAL FEEDSTOCK(21,1)\|AQUEOUS PHASE PRODUCTION(20,2)\|CO2 SCRUBBING(19,2)\|BRUCITE CARBONATION(19,1)\|CONTEMPORARY RESEARCH OVERVIEW(19,1)\|MAGNESIA CARBONATION(19,1)\|MAGNESIA TONNE(19,1)\|METHANEDIONE TONNE(19,1)\|MINERAL CARBONATION SCIENCE(19,1)\|OLIVINE CARBONATION(19,1)\|SEQUESTRATION METHANEDIONE(19,1)\|UNPRESSURIZED AQUEOUS CARBONATION(19,1)\|DGC REACTOR(17,2)\|BLENCOE ASSERTION(16,1)\|BRUCITE QUANTIFICATION(16,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(16,1)\|RIETVELD REFINEMENT QPA(16,1)\|SATISFACTORY MINERAL CARBONATION(16,1)\|SERPENTINE DEHYDROXYLATION(16,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(16,1)\|ALKALI METAL(15,15)\|BICARBONATE ION(15,3)\|MAGNESIUM SILICATE CONVERSION(14,3)\|OLIVINE POWDER(14,2)\|ANTHROPOGENIC OXIDATION(14,1)\|CARBONATION REACTOR(14,1)\|INTENSE PREPROCESSING(14,1)\|MAGNESIA DISSOLVE(14,1)\|MAGNESIA POWDER SUSPENSION(14,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(14,1)\|MINERAL CARBONATION REACTION(14,1)\|MINERAL SEQUESTRATION(14,1)\|OLIVINE DIGESTION(14,1)\|PROPOSED MINERAL CARBONATION(14,1)\|SCALABILITY EXPERIMENT(14,1)\|CO2 REMOVAL(13,4)\|STEP CONDITION(13,2)\|WOLLASTONITE(12,4)\|BRUCITE DISPERSION(12,1)\|BRUCITE POWDER SEPARATION(12,1)\|BRUCITE SOLUBILITY(12,1)\|CARBONACEOUS FOSSIL FUEL(12,1)\|CO2 TONNE(12,1)\|ELEMENTAL CONSTITUENT(12,1)\|HUGE ENERGY PENALTY(12,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(12,1)\|MASTER THESIS(12,1)\|MINERAL DIGESTION(12,1)\|MINERALOGICAL SITE(12,1)\|OVERNIGHT SHUTDOWN(12,1)\|SILICATE MINERAL CARBONATION(12,1)\|STIRRED TEFLON VESSEL(12,1)\|UTILIZATION OPTION(12,1)\|VESSEL PRESSURIZATION(12,1)\|ALKALI METAL COMPOUND(11,9)\|ALKALINE EARTH SILICATE(11,5)\|EXPERIMENTAL PATTERN(11,2)\|INORGANIC POWDER(11,2)\|METHANEDIONE SOURCE(11,2)\|UNPRESSURIZED CONTINUOUS MODE(11,2)\|AMBIENT ATMOSPHERIC PRESSURE(10,6)\|EXCESS CONSUMPTION(10,2)\|ROTAMETER(10,2)\|ALKALINE REAGENT(10,1)\|AMBIENT UNPRESSURIZED CONDITION(10,1)\|AQUEOUS MAGNESIA(10,1)\|BRUCITE CONVERSION(10,1)\|BRUCITE MINOR PHASE(10,1)\|CO2 METER(10,1)\|CO2 TRANSPORT(10,1)\|CYLINDER PREMIX(10,1)\|DIGESTION VESSEL(10,1)\|DUNITE POWDER(10,1)\|INLET CO2(10,1)\|MAGNESIA FORMATION(10,1)\|MAGNESIA YIELD(10,1)\|MAGNESIUM ION(10,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(10,1)\|MAGNESIUM SILICATE MINERAL POWDER(10,1)\|METAL SILICATE CARBONATION(10,1)\|MINERAL HYDROXIDE(10,1)\|MOLE RATION(10,1)\|OCCASIONAL MEASUREMENT(10,1)\|PARTICLE ATTRITION(10,1)\|PREMIX CYLINDER(10,1)\|PRESSURIZATION DEPRESSURIZATION(10,1)\|SAMPLE XRD PATTERN(10,1)\|SLURRY CIRCULATION(10,1)\|SLURRY DROPLET SOLUTION(10,1)\|STABLE MINERAL CARBONATE(10,1)\|STOICHIOMETRIC CONVERSION(10,1)\|STOICHIOMETRIC MOLAR RATIO(10,1)\|VALUABLE MINERAL(10,1)\|WATER CARBONATION REACTION(10,1)\|DIGESTION(9,5)\|TEMPERATURE ELEVATION(8,4)\|BICARBONATE SOLUTION(8,2)\|CAUSTIC ALKALI METAL HYDROXIDE(8,2)\|LITER WATER(8,2)\|MODEL CALCULATION(8,2)\|MOLALITY(8,2)\|PRODUCTION THROUGHPUT(8,2)\|SEAWATER(8,2)\|ABUNDANT SOURCE(8,1)\|ACIDIC PRETREATMENT(8,1)\|AGEING(8,1)\|ALKALI TREATMENT(8,1)\|ALKALINE PH(8,1)\|AMBIENT ATMOSPHERE(8,1)\|BRUCITE MAJOR PHASE(8,1)\|BUBBLE COLUMN(8,1)\|CALCIUM SILICATE MINERAL(8,1)\|CALIBRATED GLASS TUBE ROTAMMETER(8,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(8,1)\|CO2 EMISSION DISTANT SOURCE(8,1)\|CO2 EXPENSIVE SEPARATION(8,1)\|CO2 REACTION(8,1)\|CO2 SEQUESTRATION CAPACITY(8,1)\|DOMINANT REACTION(8,1)\|DRY STOICHIOMETRIC REACTION(8,1)\|EARTH ATMOSPHERE(8,1)\|ELECTRICITY GENERATING FACILITY(8,1)\|FEED MINERAL(8,1)\|GEOLOGIC TIMESCALE(8,1)\|GLASS SOLIDIFICATION(8,1)\|HUGE SCALE(8,1)\|HYDROTHERMAL REACTION SAVE(8,1)\|INFRARED DATA LOGGER(8,1)\|INLET GAS CO2(8,1)\|INORGANIC PARTICLE(8,1)\|INTIAL(8,1)\|MAGNESIA PRODUCTION(8,1)\|MAGNESIA WEIGHT(8,1)\|MAGNESIUM BICARBONATE MG(8,1)\|MAGNESIUM SILICATE CRYSTAL(8,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(8,1)\|MAGNESIUM SILICATE PARTICLE(8,1)\|MAGNESIUM SILICATE POWDER(8,1)\|MINERAL SILICATE ACTIVATION(8,1)\|MONITORED EXIT GAS(8,1)\|NATURALLY OCCURRING FEEDSTOCK(8,1)\|NONEXCLUSIVE(8,1)\|OLIVINE REACTION(8,1)\|PRECAPTURE(8,1)\|PRIMARY INITIATIVE(8,1)\|QUANTITATIVE PHASE ANALYSIS(8,1)\|REACTION ACCELERATOR(8,1)\|REACTION SOLUBLE FRACTION(8,1)\|RELIANCE(8,1)\|SALABLE CHEMICAL(8,1)\|SEALED VESSEL(8,1)\|STIRRED BED(8,1)\|STIRRED REACTOR(8,1)\|UNPRESSURIZED REACTION VESSEL(8,1)\|UNSEPARATED FLUE GAS(8,1)\|REACTION PRODUCT(7,7)\|S1O(7,3)\|UNDERLINED NUMERAL(7,3)\|GAS MIXTURE(6,10)\|STOICHIOMETRIC RATIO(6,4)\|ABSOLUTE UNCERTAINTY(6,1)\|ALKALINE COMPOUND INPUT(6,1)\|ALKALINE SOLUTION(6,1)\|AMBIENT PRESSURE CARBONATION(6,1)\|ANTIGORITE(6,1)\|AQUEOUS PHASE CARBONATION(6,1)\|AQUEOUS REACTION(6,1)\|AUTOCLAVE(6,1)\|BOUND HYDROXIDE GROUP(6,1)\|BYPRODUCT(6,1)\|CHRYSOTILE(6,1)\|CLEAR BENEFIT(6,1)\|CO2 MASS(6,1)\|COMPACTION(6,1)\|CONCENTRATED SODIUM HYDROXIDE(6,1)\|CONCERN CAUSE(6,1)\|CONSUMPTION CONDITION(6,1)\|CONTAMINATION(6,1)\|DIFFERENCE PLOT(6,1)\|DISCOVERY(6,1)\|DISSOLUTION DISINTEGRATION(6,1)\|ECONOMIC FEASIBILITY(6,1)\|EXCESS ALKALI(6,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(6,1)\|EXPERIMENTAL PERIOD(6,1)\|FIXED BED(6,1)\|GOVERNMENT(6,1)\|\|(GB2516141)\|MAGNESIA(100,31)\|MAGNESIUM SILICATE(100,27)\|MAGNESIUM SILICATE MINERAL(100,10)\|UNPRESSURIZED VESSEL(100,5)\|ACTIVATION(100,2)\|INEFFICIENCY(97,2)\|SHELL INTERNATIONAL(73,1)\|MINERAL CARBONATION(69,4)\|DRY POWDER(67,4)\|ENERGY WASTAGE(63,1)\|MAGNESIUM SILICATE DRY POWDER(60,2)\|INDIRECT SEQUESTRATION(56,1)\|METAL MINERAL SILICATE DIGESTION(56,1)\|ALKALINE AQUEOUS LIQUID SLURRY(54,2)\|METHANEDIONE(53,37)\|ROCK(50,1)\|MOLAR RATIO(48,4)\|METHANEDIONE SEQUESTRATION(37,4)\|METALLIC MINERAL SILICATE(36,1)\|DISSOLUTION(34,8)\|AQUEOUS SOLUTION(33,13)\|INDUSTRIAL PLANT(32,1)\|MINERAL SILICATE(31,2)\|SODIUM CARBONATE(28,4)\|ALKALI METAL SILICATE(27,4)\|SOLID GLASS PRODUCT(24,4)\|FORSTERITE CAREFUL QUANTIFICATION(24,1)\|SERPENTINE FEEDSTOCK TONNE(24,1)\|FLUE GAS(22,23)\|GLASS PRODUCT(22,4)\|TEMPORAL DURATION(22,4)\|MINERAL FEEDSTOCK CARBONATION(22,1)\|ALKALI METAL HYDROXIDE(21,7)\|AQUEOUS PHASE PRODUCTION(20,2)\|ENERGY EFFICIENCY(20,1)\|SALABLE INDUSTRIAL FEEDSTOCK(20,1)\|ALKALI METAL(19,23)\|ALKALINE COMPOUND(18,6)\|BRUCITE CARBONATION(18,1)\|CONTEMPORARY RESEARCH OVERVIEW(18,1)\|MAGNESIA CARBONATION(18,1)\|MAGNESIA TONNE(18,1)\|METHANEDIONE TONNE(18,1)\|MINERAL CARBONATION SCIENCE(18,1)\|OLIVINE CARBONATION(18,1)\|SEQUESTRATING METHANEDIONE(18,1)\|SEQUESTRATION METHANEDIONE(18,1)\|UNPRESSURIZED AQUEOUS CARBONATION(18,1)\|BLENCOE ASSERTION(16,1)\|BRUCITE QUANTIFICATION(16,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(16,1)\|RIETVELD REFINEMENT QPA(16,1)\|SATISFACTORY MINERAL CARBONATION(16,1)\|SERPENTINE DEHYDROXYLATION(16,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(16,1)\|STEP CONDITION(16,1)\|MAGNESIUM SILICATE CONVERSION(14,3)\|OLIVINE POWDER(14,2)\|ANTHROPOGENIC OXIDATION(14,1)\|CARBONATION REACTOR(14,1)\|CO2 SCRUBBING(14,1)\|INTENSE PREPROCESSING(14,1)\|MAGNESIA DISSOLVE(14,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(14,1)\|MINERAL CARBONATION REACTION(14,1)\|MINERAL SEQUESTRATION(14,1)\|OLIVINE DIGESTION(14,1)\|PROPOSED MINERAL CARBONATION(14,1)\|SCALABILITY EXPERIMENT(14,1)\|CAUSTIC ALKALI METAL HYDROXIDE(12,4)\|WOLLASTONITE(12,4)\|BRUCITE DISPERSION(12,1)\|BRUCITE POWDER SEPARATION(12,1)\|CARBONACEOUS FOSSIL FUEL(12,1)\|CO2 TONNE(12,1)\|HUGE ENERGY PENALTY(12,1)\|MAGNESIA POWDER(12,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(12,1)\|MASTER THESIS(12,1)\|METASTABLE CARBONATE(12,1)\|MINERALOGICAL SITE(12,1)\|MINING HIGH COST(12,1)\|SILICATE MINERAL CARBONATION(12,1)\|STIRRED TEFLON VESSEL(12,1)\|UTILIZATION OPTION(12,1)\|VESSEL PRESSURIZATION(12,1)\|EXPERIMENTAL PATTERN(11,2)\|INORGANIC POWDER(11,2)\|METHANEDIONE SOURCE(11,2)\|UNPRESSURIZED CONTINUOUS MODE(11,2)\|ALKALINE EARTH SILICATE(10,7)\|AMBIENT UNPRESSURIZED CONDITION(10,1)\|AQUEOUS MAGNESIA(10,1)\|BICARBONATE ION(10,1)\|CO2 TRANSPORT(10,1)\|DIGESTION VESSEL(10,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(10,1)\|MAGNESIUM SILICATE MINERAL POWDER(10,1)\|METAL SILICATE CARBONATION(10,1)\|MINERAL HYDROXIDE(10,1)\|PARTICLE ATTRITION(10,1)\|PRESSURIZATION DEPRESSURIZATION(10,1)\|SAMPLE XRD PATTERN(10,1)\|SLURRY CIRCULATION(10,1)\|SLURRY DROPLET SOLUTION(10,1)\|STABLE MINERAL CARBONATE(10,1)\|STOICHIOMETRIC CONVERSION(10,1)\|STOICHIOMETRIC MOLAR RATIO(10,1)\|WATER CARBONATION REACTION(10,1)\|AMBIENT ATMOSPHERIC PRESSURE(9,6)\|DIGESTION(9,5)\|ALKALI METAL BICARBONATE(8,4)\|ALKALI METAL CARBONATE(8,4)\|TEMPERATURE ELEVATION(8,4)\|HIGH COST(8,2)\|LITER WATER(8,2)\|MODEL CALCULATION(8,2)\|MOLALITY(8,2)\|PRODUCTION THROUGHPUT(8,2)\|SEAWATER(8,2)\|ABUNDANT SOURCE(8,1)\|ACIDIC PRETREATMENT(8,1)\|AGEING(8,1)\|ALKALI TREATMENT(8,1)\|ALKALINE PH(8,1)\|BRUCITE MAJOR PHASE(8,1)\|CALCIUM SILICATE MINERAL(8,1)\|CO2 EMISSION DISTANT SOURCE(8,1)\|CO2 EXPENSIVE SEPARATION(8,1)\|CO2 REACTION(8,1)\|CO2 SEQUESTRATION CAPACITY(8,1)\|DRY STOICHIOMETRIC REACTION(8,1)\|EARTH ATMOSPHERE(8,1)\|ELECTRICITY GENERATING FACILITY(8,1)\|FEED MINERAL(8,1)\|GEOLOGIC TIMESCALE(8,1)\|GLASS SOLIDIFICATION(8,1)\|HUGE SCALE(8,1)\|HYDROTHERMAL REACTION SAVE(8,1)\|INORGANIC PARTICLE(8,1)\|INTIAL(8,1)\|MAGNESIUM BICARBONATE MG(8,1)\|MAGNESIUM SILICATE CRYSTAL(8,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(8,1)\|MAGNESIUM SILICATE PARTICLE(8,1)\|MAGNESIUM SILICATE POWDER(8,1)\|MONITORED EXIT GAS(8,1)\|NATURALLY OCCURRING FEEDSTOCK(8,1)\|OLIVINE REACTION(8,1)\|PRIMARY INITIATIVE(8,1)\|QUANTITATIVE PHASE ANALYSIS(8,1)\|REACTION ACCELERATOR(8,1)\|REACTION SOLUBLE FRACTION(8,1)\|RELIANCE(8,1)\|SALABLE CHEMICAL(8,1)\|STIRRED BED(8,1)\|STIRRED REACTOR(8,1)\|UNPRESSURIZED REACTION VESSEL(8,1)\|UNSEPARATED FLUE GAS(8,1)\|UNDERLINED NUMERAL(7,3)\|STOICHIOMETRIC RATIO(6,4)\|ALKALINE INPUT(6,1)\|AMBIENT PRESSURE CARBONATION(6,1)\|ANTIGORITE(6,1)\|AQUEOUS PHASE CARBONATION(6,1)\|AQUEOUS REACTION(6,1)\|AUTOCLAVE(6,1)\|BOUND HYDROXIDE GROUP(6,1)\|BYPRODUCT(6,1)\|CHRYSOTILE(6,1)\|CLEAR BENEFIT(6,1)\|CO2 MASS(6,1)\|CO2 REMOVAL(6,1)\|CONCENTRATED SODIUM HYDROXIDE(6,1)\|CONCERN CAUSE(6,1)\|CONSUMPTION CONDITION(6,1)\|CONTAMINATION(6,1)\|DE CARBONIZED FLUE GAS(6,1)\|DIFFERENCE PLOT(6,1)\|DISCOVERY(6,1)\|DISSOLUTION DISINTEGRATION(6,1)\|ECONOMIC FEASIBILITY(6,1)\|EXCESS ALKALI(6,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(6,1)\|FIXED BED(6,1)\|\|(GB2516141)\|MAGNESIA(100,31)\|MAGNESIUM SILICATE(100,27)\|MAGNESIUM SILICATE MINERAL(100,10)\|UNPRESSURIZED VESSEL(100,5)\|ACTIVATION(100,2)\|INEFFICIENCY(97,2)\|SHELL INTERNATIONAL(73,1)\|MINERAL CARBONATION(69,4)\|DRY POWDER(67,4)\|ENERGY WASTAGE(63,1)\|MAGNESIUM SILICATE DRY POWDER(60,2)\|INDIRECT SEQUESTRATION(56,1)\|METAL MINERAL SILICATE DIGESTION(56,1)\|ALKALINE AQUEOUS LIQUID SLURRY(54,2)\|METHANEDIONE(53,37)\|ROCK(50,1)\|MOLAR RATIO(48,4)\|METHANEDIONE SEQUESTRATION(37,4)\|METALLIC MINERAL SILICATE(36,1)\|DISSOLUTION(34,8)\|AQUEOUS SOLUTION(33,13)\|INDUSTRIAL PLANT(32,1)\|MINERAL SILICATE(31,2)\|SODIUM CARBONATE(28,4)\|ALKALI METAL SILICATE(27,4)\|SOLID GLASS PRODUCT(24,4)\|FORSTERITE CAREFUL QUANTIFICATION(24,1)\|SERPENTINE FEEDSTOCK TONNE(24,1)\|FLUE GAS(22,23)\|GLASS PRODUCT(22,4)\|TEMPORAL DURATION(22,4)\|MINERAL FEEDSTOCK CARBONATION(22,1)\|ALKALI METAL HYDROXIDE(21,7)\|AQUEOUS PHASE PRODUCTION(20,2)\|ENERGY EFFICIENCY(20,1)\|SALABLE INDUSTRIAL FEEDSTOCK(20,1)\|ALKALI METAL(19,23)\|ALKALINE COMPOUND(18,6)\|BRUCITE CARBONATION(18,1)\|CONTEMPORARY RESEARCH OVERVIEW(18,1)\|MAGNESIA CARBONATION(18,1)\|MAGNESIA TONNE(18,1)\|METHANEDIONE TONNE(18,1)\|MINERAL CARBONATION SCIENCE(18,1)\|OLIVINE CARBONATION(18,1)\|SEQUESTRATING METHANEDIONE(18,1)\|SEQUESTRATION METHANEDIONE(18,1)\|UNPRESSURIZED AQUEOUS CARBONATION(18,1)\|BLENCOE ASSERTION(16,1)\|BRUCITE QUANTIFICATION(16,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(16,1)\|RIETVELD REFINEMENT QPA(16,1)\|SATISFACTORY MINERAL CARBONATION(16,1)\|SERPENTINE DEHYDROXYLATION(16,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(16,1)\|STEP CONDITION(16,1)\|MAGNESIUM SILICATE CONVERSION(14,3)\|OLIVINE POWDER(14,2)\|ANTHROPOGENIC OXIDATION(14,1)\|CARBONATION REACTOR(14,1)\|CO2 SCRUBBING(14,1)\|INTENSE PREPROCESSING(14,1)\|MAGNESIA DISSOLVE(14,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(14,1)\|MINERAL CARBONATION REACTION(14,1)\|MINERAL SEQUESTRATION(14,1)\|OLIVINE DIGESTION(14,1)\|PROPOSED MINERAL CARBONATION(14,1)\|SCALABILITY EXPERIMENT(14,1)\|CAUSTIC ALKALI METAL HYDROXIDE(12,4)\|WOLLASTONITE(12,4)\|BRUCITE DISPERSION(12,1)\|BRUCITE POWDER SEPARATION(12,1)\|CARBONACEOUS FOSSIL FUEL(12,1)\|CO2 TONNE(12,1)\|HUGE ENERGY PENALTY(12,1)\|MAGNESIA POWDER(12,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(12,1)\|MASTER THESIS(12,1)\|METASTABLE CARBONATE(12,1)\|MINERALOGICAL SITE(12,1)\|MINING HIGH COST(12,1)\|SILICATE MINERAL CARBONATION(12,1)\|STIRRED TEFLON VESSEL(12,1)\|UTILIZATION OPTION(12,1)\|VESSEL PRESSURIZATION(12,1)\|EXPERIMENTAL PATTERN(11,2)\|INORGANIC POWDER(11,2)\|METHANEDIONE SOURCE(11,2)\|UNPRESSURIZED CONTINUOUS MODE(11,2)\|ALKALINE EARTH SILICATE(10,7)\|AMBIENT UNPRESSURIZED CONDITION(10,1)\|AQUEOUS MAGNESIA(10,1)\|BICARBONATE ION(10,1)\|CO2 TRANSPORT(10,1)\|DIGESTION VESSEL(10,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(10,1)\|MAGNESIUM SILICATE MINERAL POWDER(10,1)\|METAL SILICATE CARBONATION(10,1)\|MINERAL HYDROXIDE(10,1)\|PARTICLE ATTRITION(10,1)\|PRESSURIZATION DEPRESSURIZATION(10,1)\|SAMPLE XRD PATTERN(10,1)\|SLURRY CIRCULATION(10,1)\|SLURRY DROPLET SOLUTION(10,1)\|STABLE MINERAL CARBONATE(10,1)\|STOICHIOMETRIC CONVERSION(10,1)\|STOICHIOMETRIC MOLAR RATIO(10,1)\|WATER CARBONATION REACTION(10,1)\|AMBIENT ATMOSPHERIC PRESSURE(9,6)\|DIGESTION(9,5)\|ALKALI METAL BICARBONATE(8,4)\|ALKALI METAL CARBONATE(8,4)\|TEMPERATURE ELEVATION(8,4)\|HIGH COST(8,2)\|LITER WATER(8,2)\|MODEL CALCULATION(8,2)\|MOLALITY(8,2)\|PRODUCTION THROUGHPUT(8,2)\|SEAWATER(8,2)\|ABUNDANT SOURCE(8,1)\|ACIDIC PRETREATMENT(8,1)\|AGEING(8,1)\|ALKALI TREATMENT(8,1)\|ALKALINE PH(8,1)\|BRUCITE MAJOR PHASE(8,1)\|CALCIUM SILICATE MINERAL(8,1)\|CO2 EMISSION DISTANT SOURCE(8,1)\|CO2 EXPENSIVE SEPARATION(8,1)\|CO2 REACTION(8,1)\|CO2 SEQUESTRATION CAPACITY(8,1)\|DRY STOICHIOMETRIC REACTION(8,1)\|EARTH ATMOSPHERE(8,1)\|ELECTRICITY GENERATING FACILITY(8,1)\|FEED MINERAL(8,1)\|GEOLOGIC TIMESCALE(8,1)\|GLASS SOLIDIFICATION(8,1)\|HUGE SCALE(8,1)\|HYDROTHERMAL REACTION SAVE(8,1)\|INORGANIC PARTICLE(8,1)\|INTIAL(8,1)\|MAGNESIUM BICARBONATE MG(8,1)\|MAGNESIUM SILICATE CRYSTAL(8,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(8,1)\|MAGNESIUM SILICATE PARTICLE(8,1)\|MAGNESIUM SILICATE POWDER(8,1)\|MONITORED EXIT GAS(8,1)\|NATURALLY OCCURRING FEEDSTOCK(8,1)\|OLIVINE REACTION(8,1)\|PRIMARY INITIATIVE(8,1)\|QUANTITATIVE PHASE ANALYSIS(8,1)\|REACTION ACCELERATOR(8,1)\|REACTION SOLUBLE FRACTION(8,1)\|RELIANCE(8,1)\|SALABLE CHEMICAL(8,1)\|STIRRED BED(8,1)\|STIRRED REACTOR(8,1)\|UNPRESSURIZED REACTION VESSEL(8,1)\|UNSEPARATED FLUE GAS(8,1)\|UNDERLINED NUMERAL(7,3)\|STOICHIOMETRIC RATIO(6,4)\|ALKALINE INPUT(6,1)\|AMBIENT PRESSURE CARBONATION(6,1)\|ANTIGORITE(6,1)\|AQUEOUS PHASE CARBONATION(6,1)\|AQUEOUS REACTION(6,1)\|AUTOCLAVE(6,1)\|BOUND HYDROXIDE GROUP(6,1)\|BYPRODUCT(6,1)\|CHRYSOTILE(6,1)\|CLEAR BENEFIT(6,1)\|CO2 MASS(6,1)\|CO2 REMOVAL(6,1)\|CONCENTRATED SODIUM HYDROXIDE(6,1)\|CONCERN CAUSE(6,1)\|CONSUMPTION CONDITION(6,1)\|CONTAMINATION(6,1)\|DE CARBONIZED FLUE GAS(6,1)\|DIFFERENCE PLOT(6,1)\|DISCOVERY(6,1)\|DISSOLUTION DISINTEGRATION(6,1)\|ECONOMIC FEASIBILITY(6,1)\|EXCESS ALKALI(6,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(6,1)\|FIXED BED(6,1)\|\|(GB2515995)\|METHANEDIONE(100,32)\|SEQUESTRATING METHANEDIONE(100,4)\|INEFFICIENCY(36,2)\|SHELL INTERNATIONALE(36,1)\|ALKALINE COMPOUND(35,10)\|SEQUESTRATION METHANEDIONE(30,2)\|BLEND CONTENT(26,1)\|MINERAL CARBONATION(24,5)\|BLEND(23,1)\|ENERGY WASTAGE(23,1)\|SCALABILITY(22,1)\|METHANEDIONE SOURCE(20,2)\|FLU GAS(20,1)\|INDIRECT SEQUESTRATION(20,1)\|REACTION CHAMBER(19,4)\|CO2(18,11)\|REACTION CHAMBER BLENDING CONTENT(18,1)\|SILICATE MATERIAL(17,6)\|BLENDING SYSTEM(17,1)\|ROCK(17,1)\|METAL MINERAL SILICATE DIGESTION(16,2)\|BICARBONATE(15,2)\|MINING(14,1)\|ALKALINE EARTH SILICATE(12,5)\|MOLALITY(11,2)\|INDUSTRIAL PLANT(11,1)\|LITER WATER(10,2)\|METALLIC MINERAL SILICATE(10,2)\|METHANEDIONE SEQUESTRATION(10,2)\|TEMPORAL DURATION(8,4)\|FORSTERITE CAREFUL QUANTIFICATION(8,1)\|SERPENTINE FEEDSTOCK TON(8,1)\|AQUEOUS SOLUTION(7,5)\|FLUE GAS(6,12)\|ALKALI METAL(6,5)\|AMBIENT ATMOSPHERIC PRESSURE(6,2)\|BRUCITE CARBONATION(6,1)\|CONTEMPORARY RESEARCH OVERVIEW(6,1)\|FOSSIL CARBONACEOUS FUEL(6,1)\|METHANEDIONE TONNE(6,1)\|MINERAL CARBONATION SCIENCE(6,1)\|OLIVINE CARBONATION(6,1)\|SEQUESTERING METHANEDIONE(6,1)\|ENERGY EFFICIENCY(5,3)\|STOICHIOMETRIC RATIO(5,3)\|BRUCITE QUANTIFICATION(5,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(5,1)\|MINERAL CARBONATION REACTION(5,1)\|MINERAL SEQUESTRATION(5,1)\|OLIVINE DIGESTION(5,1)\|RIETVELD REFINEMENT QPA(5,1)\|SATISFACTORY MINERAL CARBONATION(5,1)\|SCALABILITY EXPERIMENT(5,1)\|SERPENTINE DEHYDROXYLATION(5,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(5,1)\|DISSOLUTION(4,4)\|WOLLASTONITE(4,4)\|EXPERIMENTAL PATTERN(4,2)\|ANTHROPOGENIC OXIDATION(4,1)\|BRUCITE DISPERSION(4,1)\|BRUCITE POWDER SEPARATION(4,1)\|HUGE ENERGY PENALTY(4,1)\|MAGNESIA MG(4,1)\|MASTER THESIS(4,1)\|MINERALOGICAL SITE(4,1)\|STIRRED TEFLON VESSEL(4,1)\|UNPRESSURIZED VESSEL(4,1)\|DIGESTION(3,5)\|ALKALI METAL COMPOUND(3,2)\|EXCESS CONSUMPTION(3,2)\|GAS MIXTURE(3,2)\|HIGH COST(3,2)\|MODEL CALCULATION(3,2)\|PURE WATER VAPOR PRESSURE(3,2)\|DIGESTION VESSEL(3,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(3,1)\|METAL SILICATE CARBONATION(3,1)\|MINERAL HYDROXIDE(3,1)\|SAMPLE XRD PATTERN(3,1)\|STABLE MINERAL CARBONATE(3,1)\|STOICHIOMETRIC MOLAR RATIO(3,1)\|SILICON MONOXIDE(2,9)\|UNDERLINED NUMERAL(2,3)\|ABUNDANT SOURCE(2,1)\|ACIDIC PRETREATMENT(2,1)\|ADAPTABILITY(2,1)\|ALKALI TREATMENT(2,1)\|ALKALINE COMPOUND INPUT(2,1)\|ALKALINE COMPOUND SODIUM HYDROXIDE(2,1)\|AUTOCLAVE(2,1)\|CALCIUM SILICATE MINERAL(2,1)\|CONCENTRATED SODIUM HYDROXIDE(2,1)\|CONCERN CAUSE(2,1)\|DE CARBONIZED FLUE GAS(2,1)\|DIFFERENCE PLOT(2,1)\|DISCOVERY(2,1)\|EARTH ATMOSPHERE(2,1)\|ECONOMIC FEASIBILITY(2,1)\|ELECTRICITY(2,1)\|EXCESS ALKALI(2,1)\|FEED MINERAL(2,1)\|GENERATING FACILITY(2,1)\|GEOLOGIC TIMESCALE(2,1)\|GOVERNMENT(2,1)\|HYDROTHERMAL REACTION SAVE(2,1)\|INCREASING RELIANCE(2,1)\|INSTRUMENTALITY(2,1)\|MAGNESIUM BEARING MINERAL(2,1)\|MAGNESIUM BICARBONATE MG(2,1)\|MAGNESIUM SILICATE CONVERSION(2,1)\|NATURALLY OCCURRING FEEDSTOCK(2,1)\|NONEXCLUSIVE(2,1)\|OLIVINE REACTION(2,1)\|PRIMARY INITIATIVE(2,1)\|QUANTITATIVE PHASE ANALYSIS(2,1)\|REACTION ACCELERATOR(2,1)\|REACTION SOLUBLE FRACTION(2,1)\|STIRRED REACTOR(2,1)\|UNSEPARATED FLUE GAS(2,1)\|\|(CN106573197)\|MAGNESIUM SILICATE(100,40)\|MAGNESIA(100,32)\|ACTIVATED SILICATE MINERAL(100,1)\|NONCLOSED NONPRESSURIZED CONTAINER(100,1)\|ALKALINE SLURRY(63,3)\|MIXING MAGNESIA(53,1)\|MINERAL SUBSTANCE CARBONATION(51,1)\|MAGNESIUM SILICATE ROCK(37,2)\|METHANEDIONE GAS(34,24)\|ALKALI METAL SILICATE(25,5)\|ELEMENTAL SILICON(25,1)\|DRIED ALKALI METAL HYDROXIDE(21,1)\|GLASS PHASE(20,2)\|GLASSY PHASE(20,1)\|ALKALI METAL HYDROXIDE(19,7)\|DRIED ALKALI METAL(17,1)\|SUSPENDED BRUCITE PARTICLE(15,4)\|NONSEALED NONPRESSURIZED CONTAINER(15,2)\|ALKALI METAL(14,21)\|SOLID PHASE(13,4)\|METHANEDIONE GAS SCRUBBING(12,2)\|MABELL DELGADO TORR SIE(12,1)\|MINERAL CARBONATION SCIENCE ASSESSMENT(12,1)\|INTERMEDIATE PRODUCT(11,1)\|METHANEDIONE REMOVAL(10,4)\|BRUCITE CARBONATION(10,1)\|SILICATE FEEDSTOCK TON(10,1)\|SILICATE ORE FEEDSTOCK(10,1)\|METHANEDIONE SEQUESTRATION(9,5)\|POTASSIUM HYDROXIDE(9,3)\|DGC REACTOR(9,2)\|MAGNESIA POWDER(9,2)\|DUNITE ALKALINE DIGESTION(9,1)\|METHANEDIONE SCRUBBING(9,1)\|METHANEDIONE SEQUESTRATION CAPACITY(9,1)\|METHANEDIONE TON(9,1)\|OLIVINE CARBONATION(9,1)\|TECHNOLOGY SWISS FEDERAL INSTITUTE(9,1)\|INLET METHANEDIONE(8,2)\|CO2ABSOLUTE UNCERTAINTY(8,1)\|MAGNESIA TON(8,1)\|METHANEDIONE DISSOLUTION(8,1)\|METHANEDIONE VOLUMETRIC CAPACITY(8,1)\|PURITY OLIVINE MIXING(8,1)\|CELSIUS(7,11)\|DUNITE MOLAR RATIO(7,2)\|OLIVINE POWDER(7,2)\|SILICATE RAW MATERIAL(7,2)\|THERMOGRAVIMETRIC ANALYSIS(7,2)\|ATMOSPHERIC METHANEDIONE(7,1)\|BICARBONATE ION HCO(7,1)\|BRUCITE SOLUBILITY(7,1)\|CARBONATOR REACTOR(7,1)\|DOWNFLOW GAS CONTACTOR(7,1)\|FOSSIL ENERGY TON(7,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(7,1)\|METHANEDIONE GAS TON(7,1)\|METHANEDIONE GAS TRANSPORTATION(7,1)\|MOIST BRUCITE(7,1)\|OLIVINE DIGESTION(7,1)\|OLIVINE DISSOLUTION REACTION(7,1)\|OLIVINE FEEDSTOCK(7,1)\|OLIVINE MINING(7,1)\|SILICATE CARBONATION REACTION(7,1)\|SOCIAL ATTENTION(7,1)\|FLUE GAS(6,23)\|FORSTERITE(6,4)\|WOLLASTONITE(6,4)\|CARBONATING(6,2)\|ENERGY EFFICIENCY(6,2)\|MAGNESIUM ION(6,2)\|ABUNDANT MINERAL YIELD(6,1)\|BRUCITE DISPERSION(6,1)\|BRUCITE UTILIZATION(6,1)\|CARBONATE BYPRODUCT(6,1)\|CONTEMPORARY RESEARCH(6,1)\|CRYSTALLINE MAGNESIA LAYER(6,1)\|ECONOMIC VIABILITY(6,1)\|GENERAL CONSUMPTION(6,1)\|MAGNESIA CONVERSION(6,1)\|MAGNESIUM MINERAL CARBONATE(6,1)\|MAGNESIUM SILICATE ORE POWDER(6,1)\|METHANEDIONE LEAVE(6,1)\|NONPRESSURIZED VESSEL(6,1)\|OVERNIGHT STOPPAGE(6,1)\|SEAWATER SYNTHESIS(6,1)\|SOLID MATERIAL(6,1)\|SULFUR DIOXIDE SEQUESTRATION(6,1)\|ULTRAMAFIC ROCK RICH(6,1)\|AMBIENT ATMOSPHERIC PRESSURE(5,6)\|OUTLET GAS(5,4)\|BASIC COMPOUND(5,3)\|REACTION VESSEL PRESSURIZATION(5,3)\|LIQUID PHASE REACTION(5,2)\|ACTIVATED SILICATE(5,1)\|ALKALINE REAGENT(5,1)\|AMBIENT NONPRESSURIZED CONDITION(5,1)\|ARTOCARPUS DISSOLUTION(5,1)\|BRUCITE LIQUID SUSPENSION(5,1)\|BRUCITE QUANTITATIVE ANALYSIS(5,1)\|BRUCITE REACTION(5,1)\|CARBON DIOXIDE MINERAL SEQUESTRATION(5,1)\|CARBONATE PRECIPITATE(5,1)\|CARBONATION REACTION EQUATION(5,1)\|CARRYING OUT METHANEDIONE(5,1)\|CRUDE OIL WORLDWIDE CONSUMPTION(5,1)\|INLET GAS METHANEDIONE(5,1)\|INORGANIC PARTICLE COLUMN(5,1)\|MAGNESIA FORMATION(5,1)\|MAGNESIA YIELD(5,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(5,1)\|MAGNESIUM SILICATE DECOMPOSITION(5,1)\|MAGNESIUM SILICATE DISSOLUTION(5,1)\|METAL SILICATE CARBONATION(5,1)\|METHANEDIONE EMISSION SOURCE(5,1)\|METHANEDIONE GAS SEPARATION(5,1)\|METHANEDIONE MASS(5,1)\|METHANEDIONE REACTION(5,1)\|METHANEDIONE SEQUESTRATION AREA(5,1)\|MINED MAGNESIUM SILICATE(5,1)\|MINERAL DIGESTION(5,1)\|MINERAL DISSOLUTION(5,1)\|OLIVINE CONVERSION(5,1)\|OLIVINE REACTION(5,1)\|PREMIXING CYLINDER(5,1)\|PRESSURE COMPACTED DUNITE POWDER(5,1)\|PRIMARY INSOLUBLE MINERAL PARTICLE(5,1)\|SEQUESTRATION QUALITY(5,1)\|SHELL INTERNATIONAL(5,1)\|SILICATE MINERAL ACTIVATION(5,1)\|SLURRY CIRCULATION(5,1)\|SODIUM HYDROXIDE CONCENTRATIONS2THE(5,1)\|STACKING SITE(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|VALUABLE MINERAL(5,1)\|WIDESPREAD ATTENTION(5,1)\|BLENCOE(4,5)\|ACADEMIA(4,2)\|METHANEDIONE SEQUESTRATION REACTION(4,2)\|MG2SIO(4,2)\|MINERAL CARBONATION(4,2)\|ALKALINE COMPOUND(4,1)\|ALKALINE LIQUID SLURRY(4,1)\|ALKALINE PH(4,1)\|ALKALINE WASTE(4,1)\|AMBIENT ATMOSPHERE(4,1)\|AQUEOUS MAGNESIA SOLUTION(4,1)\|BRUCITE CONTENT(4,1)\|BUBBLE COLUMN(4,1)\|CHEMICAL THERMODYNAMIC VIEWPOINT(4,1)\|CURVING PROFILE(4,1)\|EARTH ATMOSPHERE(4,1)\|EXTENSIBILITY(4,1)\|FAVORABLE REACTION(4,1)\|FEED MINERAL(4,1)\|GAS STREAMIN(4,1)\|INORGANIC POWDER(4,1)\|MAGNESIA AQUEOUS SUSPENSION(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MEASURED METHANEDIONE(4,1)\|METAL SILICATE CATION(4,1)\|METHANEDIONE GAS VOLUME(4,1)\|NATURALLY OCCURRING FEEDSTOCK(4,1)\|NONAUTOCLAVE CONDITION(4,1)\|NONEXCLUSIVE(4,1)\|NONLIQUID(4,1)\|PASSIVATING SOLID(4,1)\|PRACTICABILITY(4,1)\|PRESSURIZATION DEPRESSURIZATION(4,1)\|PRESSURIZED CLOSED VESSEL(4,1)\|PRESSURIZED EQUIPMENT(4,1)\|PRESSURIZED REACTION(4,1)\|SALABLE CHEMICAL(4,1)\|SCREENED SAMPLE(4,1)\|SEALED CONTAINER(4,1)\|SILICATE POWDER(4,1)\|SILICON DOSE MOLAR RATIO(4,1)\|SOLID BRUCITE MG(4,1)\|SOLUBLE COMPOUND(4,1)\|STIRRED BED(4,1)\|STIRRED REACTOR(4,1)\|TEFLON VESSEL(4,1)\|THREATENING(4,1)\|MGCO(3,3)\|PURIFICATION(3,2)\|ACCESSORY(3,1)\|ACIDIC REAGENT(3,1)\|AGING(3,1)\|ALKALI TREATMENT(3,1)\|ALKALINE DIGESTION(3,1)\|ALKALINE SOLUTION(3,1)\|ANTIGORITE(3,1)\|BONDED HYDROXIDE GROUP(3,1)\|CALCIUM MAGNESIUM SILICATE MINERAL(3,1)\|CAPNOMETER(3,1)\|CARBON DIOXIDE REMOVAL(3,1)\|CARBONACEOUS FOSSIL ENERGY SOURCE(3,1)\|CARBONATION TECHNICAL DETAIL(3,1)\|CHRYSOTILE(3,1)\|CLINOCHLOREITE(3,1)\|COMMENT(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CORROSIVITY(3,1)\|DIFFERENCE CURVE(3,1)\|DIGESTION REACTION VESSEL(3,1)\|ENERGY LOSS(3,1)\|ENSTATITE(3,1)\|EXENDIN(3,1)\|EXPERIMENTAL PERIOD(3,1)\|FIXED BED(3,1)\|GEOLOGY(3,1)\|GLASS TUBE ROTAMETER(3,1)\|GOVERNMENT(3,1)\|H2O RATIO(3,1)\|INFINITY(3,1)\|MAGNESIUM BICARBONATE AQUEOUS SOLUTION(3,1)\|\|(CN106573197)\|MAGNESIUM SILICATE(100,41)\|MAGNESIA(100,34)\|ACTIVATED SILICATE MINERAL(100,1)\|NONSEALED PRESSURIZED CONTAINER(100,1)\|ALKALINE SLURRY(79,2)\|METHANEDIONE SEQUESTRATION(69,16)\|MINERAL SUBSTANCE CARBONATION(69,1)\|MAGNESIA GLASS PHASE(60,1)\|MAGNESIUM SILICATE ROCK(50,2)\|METHANEDIONE GAS(45,24)\|ALKALI METAL SILICATE(34,5)\|GLASS PHASE(27,2)\|GLASSY PHASE(27,1)\|SUSPENDED BRUCITE PARTICLE(20,4)\|NONSEALED NONPRESSURIZED CONTAINER(20,2)\|SOLID PHASE(18,4)\|MABELL DELGADO TORR SIE(17,1)\|MINERAL CARBONATION SCIENCE ASSESSMENT(17,1)\|METHANEDIONE GAS SCRUBBING(16,2)\|INTERMEDIATE PRODUCT(15,1)\|METHANEDIONE REMOVAL(14,4)\|BRUCITE CARBONATION(14,1)\|DRIED ALKALI METAL COMPOUND(14,1)\|SILICATE FEEDSTOCK TON(14,1)\|SILICATE ORE FEEDSTOCK(14,1)\|DUNITE ALKALINE DIGESTION(13,1)\|METHANEDIONE SCRUBBING(13,1)\|METHANEDIONE SEQUESTRATION CAPACITY(13,1)\|METHANEDIONE TON(13,1)\|OLIVINE CARBONATION(13,1)\|TECHNOLOGY SWISS FEDERAL INSTITUTE(13,1)\|METHANEDIONE SEQUESTRATION(12,5)\|POTASSIUM CARBONATE(12,3)\|POTASSIUM HYDROXIDE(12,3)\|DGC REACTOR(12,2)\|MAGNESIA POWDER(12,2)\|SODIUM CARBONATE(11,3)\|INLET METHANEDIONE(11,2)\|CO2ABSOLUTE UNCERTAINTY(11,1)\|MAGNESIA TON(11,1)\|METHANEDIONE DISSOLUTION(11,1)\|METHANEDIONE VOLUMETRIC CAPACITY(11,1)\|PURITY OLIVINE MIXING(11,1)\|DUNITE MOLAR RATIO(10,2)\|OLIVINE POWDER(10,2)\|SILICATE RAW MATERIAL(10,2)\|THERMOGRAVIMETRIC ANALYSIS(10,2)\|ATMOSPHERIC METHANEDIONE(10,1)\|BICARBONATE ION HCO(10,1)\|BRUCITE SOLUBILITY(10,1)\|CARBONATOR REACTOR(10,1)\|DOWNFLOW GAS CONTACTOR(10,1)\|FOSSIL ENERGY TON(10,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(10,1)\|METHANEDIONE GAS TON(10,1)\|METHANEDIONE GAS TRANSPORTATION(10,1)\|MOIST BRUCITE(10,1)\|OLIVINE DIGESTION(10,1)\|OLIVINE DISSOLUTION REACTION(10,1)\|OLIVINE FEEDSTOCK(10,1)\|OLIVINE MINING(10,1)\|SILICATE CARBONATION REACTION(10,1)\|SOCIAL ATTENTION(10,1)\|FLUE GAS(9,23)\|REACTION TEMPERATURE(9,10)\|ENERGY EFFICIENCY(9,2)\|MAGNESIUM ION(9,2)\|CELSIUS(8,9)\|FORSTERITE(8,4)\|WOLLASTONITE(8,4)\|CARBONATING(8,2)\|ABUNDANT MINERAL YIELD(8,1)\|BRUCITE DISPERSION(8,1)\|BRUCITE UTILIZATION(8,1)\|CARBONATE BYPRODUCT(8,1)\|CONTEMPORARY RESEARCH(8,1)\|CRYSTALLINE MAGNESIA LAYER(8,1)\|ECONOMIC VIABILITY(8,1)\|GENERAL CONSUMPTION(8,1)\|MAGNESIA CONVERSION(8,1)\|MAGNESIUM MINERAL CARBONATE(8,1)\|MAGNESIUM SILICATE ORE POWDER(8,1)\|METHANEDIONE LEAVE(8,1)\|NONPRESSURIZED VESSEL(8,1)\|OVERNIGHT STOPPAGE(8,1)\|SEAWATER SYNTHESIS(8,1)\|SOLID MATERIAL(8,1)\|SULFUR DIOXIDE SEQUESTRATION(8,1)\|ULTRAMAFIC ROCK RICH(8,1)\|AMBIENT ATMOSPHERIC PRESSURE(7,6)\|OUTLET GAS(7,4)\|BASIC COMPOUND(7,3)\|REACTION VESSEL PRESSURIZATION(7,3)\|LIQUID PHASE REACTION(7,2)\|ACTIVATED SILICATE(7,1)\|ALKALINE REAGENT(7,1)\|AMBIENT NONPRESSURIZED CONDITION(7,1)\|ARTOCARPUS DISSOLUTION(7,1)\|BRUCITE LIQUID SUSPENSION(7,1)\|BRUCITE QUANTITATIVE ANALYSIS(7,1)\|BRUCITE REACTION(7,1)\|CARBON DIOXIDE MINERAL SEQUESTRATION(7,1)\|CARBONATE PRECIPITATE(7,1)\|CARBONATION REACTION EQUATION(7,1)\|CARRYING OUT METHANEDIONE(7,1)\|CRUDE OIL WORLDWIDE CONSUMPTION(7,1)\|INLET GAS METHANEDIONE(7,1)\|INORGANIC PARTICLE COLUMN(7,1)\|MAGNESIA FORMATION(7,1)\|MAGNESIA YIELD(7,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(7,1)\|MAGNESIUM SILICATE DECOMPOSITION(7,1)\|MAGNESIUM SILICATE DISSOLUTION(7,1)\|METAL SILICATE CARBONATION(7,1)\|METHANEDIONE EMISSION SOURCE(7,1)\|METHANEDIONE GAS SEPARATION(7,1)\|METHANEDIONE MASS(7,1)\|METHANEDIONE REACTION(7,1)\|METHANEDIONE SEQUESTRATION AREA(7,1)\|MINED MAGNESIUM SILICATE(7,1)\|MINERAL DIGESTION(7,1)\|MINERAL DISSOLUTION(7,1)\|OLIVINE CONVERSION(7,1)\|OLIVINE REACTION(7,1)\|PREMIXING CYLINDER(7,1)\|PRESSURE COMPACTED DUNITE POWDER(7,1)\|PRIMARY INSOLUBLE MINERAL PARTICLE(7,1)\|SEQUESTRATION QUALITY(7,1)\|SHELL INTERNATIONAL(7,1)\|SILICATE MINERAL ACTIVATION(7,1)\|SLURRY CIRCULATION(7,1)\|SODIUM HYDROXIDE CONCENTRATIONS2THE(7,1)\|STACKING SITE(7,1)\|STOICHIOMETRIC PROPORTION(7,1)\|VALUABLE MINERAL(7,1)\|WIDESPREAD ATTENTION(7,1)\|BLENCOE(6,5)\|ACADEMIA(6,2)\|METHANEDIONE SEQUESTRATION REACTION(6,2)\|MG2SIO(6,2)\|MINERAL CARBONATION(6,2)\|REACTION PRODUCT MAGNESIA CONTENT(6,2)\|MGCO(5,3)\|PURIFICATION(5,2)\|ALKALINE COMPOUND(5,1)\|ALKALINE LIQUID SLURRY(5,1)\|ALKALINE PH(5,1)\|ALKALINE WASTE(5,1)\|AMBIENT ATMOSPHERE(5,1)\|AQUEOUS MAGNESIA SOLUTION(5,1)\|BRUCITE CONTENT(5,1)\|BUBBLE COLUMN(5,1)\|CHEMICAL THERMODYNAMIC VIEWPOINT(5,1)\|CURVING PROFILE(5,1)\|EARTH ATMOSPHERE(5,1)\|EXTENSIBILITY(5,1)\|FAVORABLE REACTION(5,1)\|FEED MINERAL(5,1)\|GAS STANDARD ATMOSPHERIC PRESSURE(5,1)\|INORGANIC POWDER(5,1)\|MAGNESIA AQUEOUS SUSPENSION(5,1)\|MAGNESIUM SILICATE CONVERSION(5,1)\|MEASURED METHANEDIONE(5,1)\|METAL SILICATE CATION(5,1)\|METHANEDIONE GAS VOLUME(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONAUTOCLAVE CONDITION(5,1)\|NONEXCLUSIVE(5,1)\|NONLIQUID(5,1)\|PASSIVATING SOLID(5,1)\|PRACTICABILITY(5,1)\|PRESSURIZATION DEPRESSURIZATION(5,1)\|PRESSURIZED CLOSED VESSEL(5,1)\|PRESSURIZED EQUIPMENT(5,1)\|PRESSURIZED REACTION(5,1)\|SALABLE CHEMICAL(5,1)\|SCREENED SAMPLE(5,1)\|SEALED CONTAINER(5,1)\|SILICATE POWDER(5,1)\|SILICON DOSE MOLAR RATIO(5,1)\|SOLID BRUCITE MG(5,1)\|SOLUBLE COMPOUND(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|TEFLON VESSEL(5,1)\|THREATENING(5,1)\|ALKALI METAL COMPOUND(4,11)\|ACCESSORY(4,1)\|ACIDIC REAGENT(4,1)\|AGING(4,1)\|ALKALI TREATMENT(4,1)\|ALKALINE DIGESTION(4,1)\|ALKALINE SOLUTION(4,1)\|ANTIGORITE(4,1)\|BONDED HYDROXIDE GROUP(4,1)\|CALCIUM MAGNESIUM SILICATE MINERAL(4,1)\|CAPNOMETER(4,1)\|CARBON DIOXIDE REMOVAL(4,1)\|CARBONACEOUS FOSSIL ENERGY SOURCE(4,1)\|CARBONATION TECHNICAL DETAIL(4,1)\|CHRYSOTILE(4,1)\|CLINOCHLOREITE(4,1)\|COMMENT(4,1)\|CONCENTRATED SODIUM HYDROXIDE(4,1)\|CORROSIVITY(4,1)\|DIFFERENCE CURVE(4,1)\|DIGESTION REACTION VESSEL(4,1)\|ENERGY LOSS(4,1)\|ENSTATITE(4,1)\|EXENDIN(4,1)\|EXPERIMENTAL PERIOD(4,1)\|FIXED BED(4,1)\|GEOLOGY(4,1)\|GLASS TUBE ROTAMETER(4,1)\|	(EP3129125)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising:\| a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from the group consisting of alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture;\| b. heating the dry solid-solid mixture to a temperature below 300 °C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and\| c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|2. A method as claimed in claim 1, characterized in that the liquid slurry of step c is separated into solid and aqueous solution phase products.\|3. A method as claimed in claim 1 or 2, characterized in that the method includes reacting any of the aqueous phases at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|4. A method as claimed in claim 2, characterized in that the method includes mixing the solid phase product with water and reacted at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|5. A method as claimed in claim 3 or 4, characterized in that the method includes air as the gas in the reaction.\|6. A method as claimed in claim 3 or 4, characterized in that the method includes an industrial flue gas in the reaction.\|7. A method as claimed in claim 1, characterized in that the method includes using a hydroxide or a carbonate of sodium or a potassium as the alkali metal compound in the reaction.\|8. A method as claimed in claim 1, characterized in that the method includes a serpentine or an olivine rock as the magnesium silicate mineral in the reaction.\|9. A method as claimed in claim 1, characterized in that the method includes heating the unpressurised vessel in step (b) to a temperature in the range 140C-220C.\|10. A method as claimed in claims 1, characterized in that the method includes continuously adding the magnesium silicate mineral and alkali metal compound of step (a) together allowing continuous reacting thereof under the conditions of step (b) and further continuously removing the product of step (b).\|11. A method as claimed in claim 1, characterized in that the method includes the molar ratio of substantially 2 moles of alkali metal per mole of silicon in the mixture.	(EP3129125)\|TECHNICAL FIELD\|[0001] The present disclosure relates to methods of producing activated mineral silicate for use in sequestrating Carbon Dioxide, for example from flue-gas, by utilizing a process which involves digestion of metal mineral Silicates. Moreover, the present disclosure also relates to systems for executing aforesaid methods.\|BACKGROUND\|[0002] Increasing concentrations of Carbon Dioxide (CO2) in the Earth's atmosphere have recently caused concerns, as the present concentrations are substantial at 400 p.p.m. and increasing at a rate of 4 p.p.m. per annum. A major factor contributing to such increase is the anthropogenic oxidation of carbonaceous fossil fuels, for example coal, oil and gas. The World presently consumes circa 100 million barrels of oil per day.\|[0003] There have been recent initiatives to employ more renewable energy systems, for example wind turbines and tidal power generating systems, as well as sequestration of Carbon Dioxide (CO2) from flue-gases emitted from coal burning electricity generating facilities. Thus, primary initiatives involve utilizing energy efficient technologies, increasing reliance on renewable sources, and developing technologies for long term storage of Carbon Dioxide (CO2) emissions. The latter technology field is known as Carbon Dioxide (CO2) sequestration.\|[0004] There have been significant developments in Carbon Dioxide (CO2) sequestration in recent years, and Carbon Dioxide sequestration technologies have aroused considerable interest among governments, industries and scientific communities. Earlier methods of Carbon Dioxide (CO2) sequestration suffered from various drawbacks such as risk of water contamination, and a lack of suitable storage spaces for receiving sequestrated Carbon Dioxide (CO2); these drawbacks are familiar to a person skilled in the art.\|[0005] There has been considerable interest in mineral Carbonation technologies to address aforementioned problems associated with known Carbon Dioxide (CO2) sequestration. The Masters thesis by Mabell Delgado Torróntegui at ETH in Switzerland, "Assessing the Mineral carbonation science and technology" (2010), provides an overview of contemporary research in this field of Carbon Dioxide (CO2) sequestration technology. A key principle of mineral Carbonation is also known as "mineral sequestration technology", wherein sequestration of Carbon Dioxide (CO2) is achieved by capturing Carbon Dioxide (CO2) in a form of stable mineral Carbonates. Such sequestration employs a process which is an exothermic reaction of a metal Oxide and Carbon Dioxide (CO2) to form stable Carbonate materials as provided in a reaction formula (1):\| MO + CO2 => MCO3 + Heat (1)\|wherein M is a metal, preferably an alkaline earth metal such as Calcium or Magnesium.\|[0006] Most suitable and naturally abundant sources of these metal Oxides are Magnesium or Calcium Silicate minerals such as Olivine, wollastonite, and Serpentine. The Carbonation reactions of these minerals are as follows:\| Olivine:\| Mg2SiO4 + 2CO2 => 2MgCO3 + SiO2 + 89 kJ mol-1CO2 (2)\| Serpentine:\| Mg3Si2O3(OH)4 + 3CO2 => 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol-1CO2\| Wollastonite:\| CaSiO3 + CO2 => CaCO3 + SiO2 + 90 kJ mol-1CO2 (4)\|[0007] Although the above reactions (2) to (4) are thermodynamically favourable, the reactions in nature have, however, relatively slow reaction rates in a geologic time scale, and are unsuitable for industrial processes. Efforts have been made to try to accelerate these reactions. However, the efforts suffer from various limitations, such as energy wastage and a high cost of mining and transporting large amounts of rock, as well as industrial and environmental inefficiencies. Moreover, the mineral Silicates are not easily obtainable in suitable quantities and formats for allowing satisfactory mineral Carbonation to be achieved.\|[0008] In a published US patent no. US7604787B2 (MAROTO-VALER), "Process for sequestering Carbon Dioxide and Sulphur Dioxide", there is described a method of reacting a Silicate-based material with an acid to form a suspension, which is then combined with Carbon Dioxide to produce a metal salt, silica and regenerating acid in solution. This method has drawbacks of being environmentally harsh and inefficient. Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for removal and Capture of Carbon Dioxide from Flue Gases".\|[0009] Although, the prior art disclosures have been able to address some of the problems of mineral Carbonation through their indirect sequestration processes, there are several remaining problems which have not yet been resolved. Such remaining problems pertain to industrial scalability, environmental efficiency, and cost.\|[0010] Lately, research effort has focused upon Carbon Dioxide (CO2) sequestration by 'direct' Carbonation of Olivine or Serpentine. In these recent methods, Carbon Dioxide (CO2) is sequestered without acid pretreatment of Silicate feedstock. An Olivine reaction is:\| Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 (5)\|[0011] Moreover, for Serpentine, a corresponding reaction is:\| Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O (6)\|[0012] Experiments to determine the kinetics of these reactions (5) and (6) have shown that such reactions also suffer from poor energy efficiency and a high cost when up-scaled to an industrial plant. In order to accelerate the reactions (5) and (6), high temperatures in a range of 600°C to 650 °C are required. In a fuel-fired industrial power plant, attainment of such high temperatures would translate to a requirement of approximately 200 kW-h of electricity per tonne of Serpentine feedstock. Moreover, with a fossil fuel containing 1 tonne of Carbon, nearly 3.7 tonnes of Carbon Dioxide (CO2) is produced. Each tonne of Carbon Dioxide (CO2) consumes more than 2 tonnes of Serpentine during Carbonation. Combined with a pre-capture step to separate and pressurise CO2 from flue gas, the power required for Serpentine dehydroxylation Is around 20-30% of total power output from such fuel-fired industrial power plant. All these considerations lead to a huge energy penalty threatening the economic feasibility of this sequestration process.\|[0013] In a published US patent no. US8114374B2 (BLENCOE), "Carbonation of metal Silicates for long-term CO2 sequestration", there is described a method (hereinafter "Blencoe's method") of reacting a Silicate with an alkali metal hydroxide in an aqueous solution. The reaction with Carbon Dioxide (CO2) is then used to carbonate the metal formerly contained in the metal Silicate. This method has drawbacks of inefficiencies and poor overall Carbon capture properties. Blencoe's method comprises three steps:\| (1) reacting a metal silicate with a caustic alkali-metal hydroxide to produce a hydroxide of the metal formerly contained in the silicate;\| (2) reacting carbon dioxide with at least one of a caustic alkali-metal hydroxide and an alkali-metal silicate to produce at least one of an alkali-metal carbonate and an alkali-metal bicarbonate; and\| (3) reacting the metal hydroxide product of step (a) with at least one of the alkali-metal carbonate and the alkali-metal bicarbonate produced in step (b) to produce a carbonate of the metal formerly contained in the metal silicate of step (a).\|[0014] In Blencoe's first step (1), the alkali-metal hydroxide is in aqueous solution which limits the maximum reaction temperature to the vapour pressure of the aqueous solution at the pressure under which the reaction is carried out. A low reaction temperature limits the reaction rate at atmospheric pressure, while use of a pressurised vessel increases process costs. Alkali-metal hydroxides, such as NaOH and KOH, used in steps (1) and (2) are energy intensive and expensive chemicals to manufacture. In Blencoe's second step (1), alkali-metal hydroxide, additional to that used in step (1), is used to react with Carbon Dioxide. In Blencoe's second and third steps (2) and (3), an elevated pressure is required, namely having implied costs of a pressure vessel, in the range between the vapour pressure of water at the reaction temperature and Bar. It is doubtful that the overall process described is able to sequester more Carbon Dioxide as a metal carbonate than is generated as a consequence of manufacture of the alkali-metal hydroxides consumed in the process, or that the process is any cheaper to operate than Carbon Dioxide sequestration processes described in the prior art.\|[0015] Therefore, there is an urgent need to develop a process which is energy efficient, has a high throughput and is more cost effective than the prior art so that it can be used industrially.\|[0016] From the foregoing, it will be appreciated that the known methods of processing and the systems for mineral carbonation and Carbon Dioxide (CO2) sequestration, are neither optimal in their manner of operation nor adaptable to broader applications in a cost effective manner.\|SUMMARY\|[0017] The present invention seeks to provide an improved method of activation of magnesium silicate minerals by conversion to magnesium hydroxide.\|[0018] This present embodiment of the invention allows for a method of large scale industrial use and continuous carbonation without advanced pressure chambers or equipment.\|[0019] The present invention provides a method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, wherein the method comprises:\| a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from a group comprising alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture;\| b. heating the dry solid-solid mixture to a temperature below 300°C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and\| c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|[0020] Optionally, the method includes the liquid slurry of step c being separated into solid and aqueous solution phase products.\|[0021] Optionally, the method includes reacting any of the aqueous phases at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|[0022] Optionally, the method includes mixing the solid phase product with water and reacted at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|[0023] Optionally, the method includes air or flue gas as the gas in the reaction. This allows for a very simple and cost-effective solution utilizing what is available at the site of operation.\|[0024] Optionally, the method includes using a hydroxide or a carbonate of sodium or a potassium as the alkali metal compound in the reaction.\|[0025] Optionally, the method includes a serpentine or an olivine rock as the magnesium silicate mineral in the reaction. Further, optionally, the method includes heating the unpressurised vessel in step (b) to a temperature in the range 140 °C - 220 °C.\|[0026] Optionally, the method includes continuously adding the magnesium silicate mineral and alkali metal compound of step (a) together allowing continuous reacting thereof under the conditions of step (b) and further continuously removing the product of step (b).\|[0027] Optionally, the method includes the molar ratio of substantially 2 moles of alkali metal per mole of silicon in the mixture.\|[0028] Additional aspects, advantages, features and objects of the present invention would be made apparent from the drawings and the detailed description of the illustrative embodiments construed in conjunction with the appended claims that follow. It will be appreciated that features of the present invention are susceptible to being combined in various combinations from different embodiments without departing from the scope of the present invention as defined by the appended claims.\|DESCRIPTION OF DRAWINGS:\|[0029] The summary above, as well as the following detailed description of illustrative embodiments, is better understood when read in conjunction with the appended drawings. For the purpose of illustrating the present invention, exemplary constructions of the disclosure are shown in the drawings. However, the present invention is not limited to specific methods and apparatus disclosed herein. Moreover, those in the art will understand that the drawings are not to scale. Wherever possible, like elements have been indicated by identical numbers.\| FIG. 1 is an illustration of a flow chart of a digestion Step 1 involving alkaline digestion of Serpentine or Olivine to convert them to Brucite and Silica;\| FIG. 2 is an illustration of a flow chart of a Carbonation step 2 involving direct Carbonation of Brucite, namely Magnesium Hydroxide, with flue-gas to form Magnesium Carbonate;\| FIG.3a and 3b are illustrations of XRD patterns of selected samples, wherein solid products from dissolution of Dunite, namely a form of Olivine, using Sodium Hydroxide (NaOH) solution of concentration in a range of 15 to 40 mol/kg (left), and using Sodium Hydroxide (NaOH) solution of concentration 50 mol/kg (right) solutions. In the illustrations, following abbreviations are employed: Fo = Forsterite, Brc = Brucite, Clc = Clinochlore, En = Enstatite, Srp = Serpentine, Tlc = Talc, Spl = Spinel;\| FIG. 4a and 4b are illustrations of TG (4a) and DTG (4b) curves of selected samples: solid products from dissolution of Dunite at a temperature of 180°C for 15 for 6 hours with different concentrations of Sodium Hydroxide (NaOH) solution;\| FIG. 5 is a graph wherein there are shown Mg(OH)2 concentrations in solid products based on TG results: Dunite dissolved at a temperature of 180°C with different concentrations of Sodium Hydroxide (NaOH) solution, namely measured as moles of NaOH per kg of water. From the graph, it will be appreciated that the proportion of Dunite, namely magnesium silicate, converted to Brucite, namely magnesium hydroxide, increases approximately linearly with increase in NaOH concentration; extrapolation of this graph indicates that the proportion of Brucite in the solid product should approach 100% above a NaOH concentration >70mol/kg, namely equivalent to a NaOH: H2O ratio >1.26;\| FIG. 6 is an illustration of XRD patterns of solid products from dissolution of Dunite at 180 °C with Sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg solution, for different temporal durations;\| FIG. 7a and 7b are illustrations of TG (7a) and DTG (7b) curves of solid products from dissolution of Dunite at a temperature of 180° C with sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg for different temporal durations;\| FIG. 8 is a graph in which there is shown Magnesium Hydroxide Mg(OH)2 concentration in solid products based on TG results: Dunite dissolved at a temperature of 180 °C with a molar concentration of Sodium Hydroxide (NaOH) solution being 40 mol/kg for different durations;\| FIG. 9 is an illustration showing Rietveld Refinement QPA of raw Dunite, wherein: data points profile = experimental pattern; continue profile = calculated model (above); difference plot (below);\| FIG. 10 is an illustration showing Rietveld Refinement QPA of dissolved Dunite spiked with 10 wt% Silicon, wherein: data points profile = experimental pattern; continue profile = calculated model; and\| FIG. 11a and 11b are illustrations showing Brucite quantification with Rietveld Refinement and TGA (FIG. 11a), wherein Forsterite and Brucite concentrations were obtained via Rietveld Refinement QPA of selected samples (FIG. 11b).\| FIG. 12a and 12b depict experimental data concerning the removal of CO2 by means of Brucite powder in aqueous suspension, specifically the resulting CO2 level for a monitored exit gas after processing.\|[0030] In the accompanying drawings, an underlined number is employed to represent an item over which the underlined number is positioned or an item to which the underlined number is adjacent. A non-underlined number relates to an item identified by a line linking the non-underlined number to the item. When a number is non-underlined and accompanied by an associated arrow, the non-underlined number is used to identify a general item at which the arrow is pointing.\|DETAILED DESCRIPTION OF EMBODIMENTS\|[0031] The following detailed description illustrates embodiments of the present disclosure and ways in which they can be implemented.\|[0032] In FIG. 1, there is shown a digestion process 100, wherein there occurs alkaline digestion of a Silicate-based material, a naturally occurring feedstock containing magnesium or calcium silicate, such as Serpentine, Olivine, Dunite, and/or Wollastonite 101. The process 100 results in reaction products being generated, namely a conversion to Brucite and Silica in a case of Olivine 101 being a feed mineral employed. In the reaction, Olivine 101 is fed into a stirred reactor 102 together with an alkali 103 and heat is provided from a heat source 104. The alkali is beneficially selected from a mineral Hydroxide. Among the many metal Hydroxides that can find utility in this reaction, a preferable alkali used is Sodium Hydroxide (NaOH) .\|[0033] The reaction mixture of the digestion process 100 comprises a stoichiometric ratio between the soluble silicate based material and the solid hydroxide of the alkaline earth compound of about 1:2. This stoichiometric ratio aims to minimise the input of the alkaline compound, such as Sodium Hydroxide (NAOH), into the initial reaction mixture. This limits the regeneration of Sodium Hydroxide (NaOH) from carbonates at the end of the reaction, which is costly and time consuming. The reaction mixture is a dry mixture.\|[0034] According to a further embodiment, the reaction mixture is a solid-state dry mixture of a powder of the alkaline-earth silicate and the alkali-metal compound, in the stoichiometric ratio of one mole of silicon, namely in the silicate, per two moles of alkali-metal. Solid alkali-metal compounds, such as NaOH, KOH and Na2CO3, have high melting points, namely 318°C, 406°C and 851 °C, respectively. Using an aqueous system, such as taught by Blencoe, would therefore be expected to be essential to achieving mixing and reaction at temperatures below 300 °C. Surprisingly, in experiments using NaOH and Serpentine, namely magnesium silicate, it is found that a dry solid state mixture of the two rapidly melted, mixed and reacted to form magnesium hydroxide in an unpressurised vessel at temperatures as low as 180°C, namely well below the melting temperature of NaOH, namely 318°C, or of Serpentine, namely >1700 °C. Unlike Olivine, Serpentine has a crystal structure that contains chemically bound hydroxide groups, and it is believed that these groups may facilitate the dry stoichiometric reaction to form magnesium hydroxide.\|[0035] Dunite can also be used to yield Mg(OH)2 via solid state reaction, with a preferable ratio of Dunite to NaOH in a mole ratio of 1:2, at a temperature around 180 °C. Experiments conducted with a range of Dunite: NaOH mole ratios of 1:0.5, 1:1, 1:.5 and 1:2, where the powder has been formed into pellets by compaction with a hand press (3 tonnes for 1 minute for compression), returned results indicating a linear increase of Mg(OH)2 production with increase of NaOH, to a maximum weight percentage of Mg(OH)2 in the reaction products of around 46.7%. Reducing the amount of NaOH significantly lowered the extraction efficiency of the process.\|[0036] In contrast, results of non-inventive experiments, as provided in FIGs. 3a, 3b, 5, with aqueous NaOH and Olivine show that minimum reaction conditions of a temperature of 180°C and a NaOH concentration of 40mol/kg are substantially required to form magnesium hydroxide; this system requires a pressure vessel to reach a required reaction temperature.\|[0037] For the case of Dunite samples, comparison of the results cited above with alkaline digestion of Dunite with 50mol/kg NaOH aqueous system at 180°C under a similar time period, show that the yield of Mg(OH)2 via solid state reaction (55% to 62%) was on a par with that produced using the aqueous system (between 58% and 66%). The alkaline digestion with 50mol/kg NaOH required significantly more NaOH per 1 gram of Dunite processed such that the solid state reaction effected a 97% to 99% reduction of NaOH consumption. Additional experimental results comprising Dunite as a sample component are detailed later.\|[0038] Generally stated, it has been demonstrated that it is possible to extract Mg(OH)2 from magnesium containing silicate minerals via solid state reaction with NaOH and that the consumption of the alkaline reactant can be reduced, achieving significant yield of reaction. An additional advantage is the reduction of water consumption which would be needed for an aqueous process.\|[0039] Moreover, results have also shown, namely in FIG. 5, that without water, the NaOH concentration (mol/kg) effectively approaches infinity and might therefore be expected to approach 100% conversion of magnesium silicate to magnesium hydroxide. Compared to the aqueous reaction system, as exemplified by Blencoe, clear benefits of the non-aqueous dry-mixture and stoichiometric system using Serpentine are that:\| (i) no pressure vessel is required;\| (ii) melting and mixing surprisingly take place at 180 °C, to enable a rapid reaction at a rate similar to an aqueous system;\| (iii) a highest possible concentration and activity of NaOH is enabled, leading to a faster and more complete reaction than possible in an aqueous system at a similar temperature;\| (iv) the NaOH is totally consumed in a reaction with silicate to form solid sodium silicate, so that no subsequent process for recovery of excess NaOH from the reaction products is required;\| (v) Serpentine provides any water required for the stoichiometric conversion to magnesium hydroxide from its structural hydroxide groups, so that no free water needs to be added to the reaction system;\| (vi) the products of reaction, containing no excess NaOH, are a solidified glass which is substantially less caustic than in the aqueous process and are therefore much safer to handle;\| (vii) sodium silicate is readily separated from the products of reaction by dissolution and filtration, and is available without contamination by NaOH; and\| (viii) the process can be more readily and cheaply carried out at remote Serpentine or Olivine mine sites where water may not be available.\|[0040] Further, in the prior art of Blencoe it is described how the initial step (a) can be conducted at a pressure slightly below the vapour pressure of pure water for the temperature of that step. Blencoe does not claim a preferred temperature or pressure or aqueous solution composition for that initial step (a), but in a table of experimental results shows that all reactions in which serpentine or olivine are converted to a major phase of brucite are done in aqueous solution in a pressure vessel at a temperature of 200 °C and pressure <15atm. One experiment conducted at a temperature of 22 °C and 1atm pressure for 72hrs results in conversion to a minor phase of brucite; subsequent additional reaction at 200 °C and < 15bar then converts substantially to brucite with a minor residual phase of serpentine. Notwithstanding Blencoe's assertion of the technological and commercial advantage of avoiding pressure-intensifying equipment, at the effective reaction temperature of 200 °C for Blencoe's step (a), the vapour pressure of pure water is just above bar indicating that a pressure vessel must be used in this step. The current invention allows for the method and system to operate without expensive and complicated equipment used in Blencoe to operate at higher than atmospheric pressure.\|[0041] In the example of magnesium carbonates being produced according to the described method, a wide range of compounds including soluble magnesium bicarbonate Mg(HCO3)2 is produced in solution, but generates no separate water in the carbonation reaction:\| 2CO2+ Mg(OH)2 = Mg.(HCO3)2 (7)\|[0042] The preferred alkali 103 for this digestion process is beneficially Sodium Hydroxide or Potassium Hydroxide. It is also possible to use Sodium Carbonate, Sodium Bicarbonate, Potassium Carbonate and Potassium Bicarbonate as the alkali for the digestion process.\|[0043] The heat source 104 is employed to raise a temperature of the digestion process, whilst stirring of the mixture is implemented, to a temperature of less than 250 °C, and for a temporal period of less than 6 hours. A preferred range of temperature is from 140 °C to 220 °C. The reaction can be best performed with the temperature being less than 200 °C, and most preferentially at around 180 °C, throughout the process, as shown in the results FIG. 4 to FIG. 8. The digestion vessels used are most suitably Teflon (PTEE) to withstand hot-conc-NaOH with the maximum operating temperature usually specified at 220 °C. Experiments with Magnesium silicate mineral feedstocks have been showing excellent results for this process.\|[0044] This digestion process is preferably carried out at a pressure of less than Bar, wherein 1 Bar corresponds to nominal atmospheric pressure at sea-level. The reaction can be more preferably carried out at a pressure less than 10 Bar. The reaction can be furthermore preferably be carried out at pressure conditions lower than the vapour pressure of pure water at the temperature of reaction. The benefit of not having to use high pressure vessels to carry out hydrothermal reactions saves cost and also improves the applications of the technology in industrial applications at very high volumes and large scale installations.\|[0045] The process, after digestion of Olivine, is shown in equation 112. Here, the Brucite (MgOH2) 107, solid phase, is separated from a Silicate solution 108. Thereafter, the Silica precipitation process is carried out as depicted in the equations 113 and 112. The process, namely acid precipitation, can be carried out by adding either Carbon Dioxide (CO2) or acid 110. Excess alkali 111 is recovered and fed back to a chamber of the reactor 102. Performing the digestion process at ambient atmospheric pressure conditions avoids a need to employ equipment to increase pressure, for example an autoclave, and allows large scale, continuous sequestration of industrial Carbon Dioxide (CO2) emissions to be achieved. Avoiding the requirement for any pressurised containment of the reaction steps, provides several benefits:\| (i) much cheaper and simpler reaction vessels can be used;\| (ii) it is easier and cheaper to incorporate mixing, stirring and/or particle attrition to enhance reaction rates within an unpressurised reaction vessel;\| (iii) energy usage, namely energy wasted in pressurisation/ depressurisation, is lower;\| (iv) product throughput is faster, namely a need for time to pressurise is avoided; and\| (v) while pressurised reaction systems tend to operate in batch mode, it is much easier to configure each step, and also the overall process, as a continuous operation in an unpressurised system.\|[0046] Continuous operation is generally recognised by process engineers as preferable to batch operations because:\| (a) reaction parameters such as temperature, pH and reactant concentrations are easier to maintain at fixed optimum levels; and\| (b) residence times are shorter, thereby enabling process equipment to be smaller and cheaper and product throughput higher.\|[0047] In FIG. 2, there is provided an illustration of the details of a Carbonation process 200 as also depicted in equations 206 and 207. The Brucite (MgOH2) powder 205 is fed into a continuous reactor 201, together with a flue-gas 204. The de-carbonised flue gas 202 and Magnesium Carbonate (MgCO3) powder 203 are the reaction products of this Carbonation process 200.\|[0048] In a further embodiment of the present invention, Mg(OH)2 (Brucite) powder is provided as added to water to form an aqueous suspension which is then used at ambient temperature and pressure to scrub CO2 from a gaseous mixture of nitrogen (N2) and CO2.The scrubbing process using wet-Brucite which simultaneously removes the CO2 from the gas mixture and converts the Brucite to magnesium carbonates. Substantial removal and conversion can be achieved such that most, if not all, of the CO2 is taken out of the gas mixture and most, if not all, of the Brucite is converted.\|[0049] Following a particular example of such a further embodiment of the invention, consider the following experiment:\|A gas mixture of (nitrogen) N2 containing 4-5% CO2 (carbon dioxide, cylinder pre-mix) was bubbled continuously at a fixed flow-rate (around 2.25 litres/minute) through a fixed circulating volume (around 10 litres) of water (pre-saturated before the experiment with 5%CO-N2) containing a suspension of magnesium hydroxide powder (0.871 mol, 50.8 grams). The CO2 concentration in the exit gas was initially zero (as it was totally removed by reaction with Brucite) and was monitored as the suspended Brucite particles were consumed in the reaction to form dissolved magnesium bicarbonate. Periodic samples of the circulating liquid were taken to monitor change in pH and magnesium ion concentration. The experiment was concluded when the concentration of CO2 in the exit gas had increased to equal that of the inlet concentration, indicating that no further reaction was occurring. The experiment took approximately 12 hours to complete and was run over the course of two days with an overnight shut-down.\|[0050] A Down-flow Gas Contactor (DGC, WRK Design & Services Ltd) with a liquid volume of around 10 litres was used as the gas-liquid reactor. In this reactor, the gas-mixture at atmospheric pressure entered at the top of a bubble column, entrained in a downward circulating liquid flow. The rate of liquid recirculation in the DGC reactor (around 10 litres/min) was adjusted to maintain a stable bubble-liquid interface. The CO2-depleted gas exited from the bottom of the column after reaction and separation from the recirculating liquid phase. Gas flow rate was measured by calibrated glass tube rotammeter at a fixed 2.25 litres/minute (atmospheric pressure).\|[0051] Concentration of CO2 was measured using a calibrated inline infrared datalogger (range: 0-5 % CO2 measured to nearest 0.25 %). Temperature was ambient, in a range of 9.5-11 °C. Solution pH was in a range of pH 8.2-8.9.\|[0052] The DGC reactor provides a large and dynamic interfacial area between gas bubbles and circulating liquid. During the course of the experiment, CO2 dissolves from the gas (g) into the liquid (I) phase (or aqueous phase, aq) and reactions occur with the suspended Brucite particles (solid phase being labelled as s):\| CO2 (g) = CO2 (aq) (E1)\| CO2 (aq) + H2O(I) = H2CO3 (aq) (E2)\| H2CO3 (aq) = H+(aq) + HCO3-(aq) (E3)\| HCO3-(aq) = H+(aq) + CO32-(aq) (E4)\| Mg(OH)2(s) = Mg2+(aq) + 2OH-(aq) (E5)\| Mg(OH)2(s) + CO2(aq) = MgCO3(s) + H2O(I) (E6)\| Mg(OH)2(s) + 2CO2(aq) = Mg2+(aq) + 2HCO3-(aq) (E7)\| Mg2 +(aq) + CO32-(aq) = MgCO3(s) (E8)\| MgCO3(s) + CO2(aq) = Mg2+(aq) + 2HCO3-(aq) (E9)\|[0053] In alkaline solution, Brucite solubility is well known to be negligible while CO2 dissolves readily. In the pH range of the experiment, pH falls in the range 8.2-8.9, the predominant form of carbon in solution is the bicarbonate ion, HCO3- (aq). The dominant reactions in this situation may therefore be expected to be:\| CO2 (g) + H2O(I) = H+(aq) + HCO3-(aq) (E10)\|and\| Mg(OH)2(s) + 2H+(aq) = Mg2+(aq) + 2H2O(I) (E11)\|[0054] At higher pH, where carbonate ions dominate, the formation of solid magnesium carbonate phases would be expected and, moreover, may precipitate on the surface of the suspended Brucite particles, blocking the Brucite to further reaction with CO2.At lower pH, dissolution of CO2 would be inhibited. However, at pH 8-9, where bicarbonate ions are greatly in excess of carbonate ions, formation of solid magnesium carbonate phases should be minimal, with the result that suspended Brucite particles should fully react with CO2, ideally in a mole ration of 1:2, to form an aqueous solution of magnesium bicarbonate.\|[0055] CO2 concentrations in exit gas were data-logged continuously. Occasional measurements of (fixed) inlet CO2 concentration were taken. The resulting data is shown in the two charts: one for day 1 detailing results 1200 (Fig. 12a) and one for day 2 detailing results 1201 (Fig 12b), 5 showing CO2 concentration (%CO2) versus time.\|[0056] Analysis: The total amount of CO2 removed from the inlet gas is calculated from the measured gas flow-rate and the measured difference between inlet and outlet gas concentration: \|[0057] Uncertainty in the flow-rate measurement (rotameter) is estimated from rotameter specifications as 3 %. The CO2 meter was able only to measure to the nearest 0.5 % in a CO2 concentration range of 0-5 %. Additionally, the inlet gas CO2 concentration from the pre-mix cylinder was measured at different times in the experiment as 4 % and 5 %. Absolute uncertainty in the measured % CO2 concentration change is estimated at 0.7 % CO2.\|[0058] The total amount of CO2 removed from the inlet gas during the 12 hour course of the experiment was measured as 1.87 moles (± 0.2 moles). Within experimental error, this is the amount of CO2 expected to be removed if all 0.871 moles of the initial Brucite had reacted with CO2 to form dissolved magnesium bicarbonate according to reaction (E7) above. Within the limits of measurements errors, results show that 100 % utilisation (carbonation) of Brucite is feasible when wet-scrubbing 5 % CO2-N2 gas mixture.\|[0059] Results also show that for the first 3.5 hours of the 12 hour experimental period, removal of CO2 from the inlet 5 % CO2-N2 gas mixture was 100 %. Over the first 6 hrs (first day), CO2 removal averaged 93 % and over the full 12 hours averaged 62%. Results show unequivocally that a Brucite-water suspension can fully scrub CO2 from dilute gas mixtures.\|[0060] It may be expected that in a future industrial CO2 scrubbing system, in which the rates of water, Brucite and CO2 addition may be controlled to maintain pH within a range of around pH 8 to pH 9, and where magnesium bicarbonate is removed, continuous removal of CO2, controllable up to 100%, should be possible and/or simultaneous with up to 100% conversion of Brucite to magnesium carbonates.\|[0061] Referring to "unpressurized" mentioned in the foregoing, it is optionally feasible to vent apparatus for implementing embodiments of the present disclosure directly to ambient atmosphere, namely substantially 1 Bar pressure, thereby avoiding a need for using expensive pressure vessels. However, optionally, embodiments of the present disclosure are operated in a substantially unpressurized manner at pressures in a range of 0.5 Bar to 10.0 Bar, more optionally in a range of 0.8 Bar to 5.0 Bar, and yet more optionally in a range of 0.9 Bar to 2.0 Bar. It will be appreciated that "pressurized", in contradistinction, refers to pressures, for example, in excess of 20 Bar, in excess of 50 Bar, or even in excess of 100 Bar.\|[0062] For example, the first steps of the process in which a mined magnesium silicate mineral is converted into magnesium hydroxide can be carried out at the mine site, while, without a need for elevated temperatures or pressures for reaction, the final step in which CO2 in flue-gas reacts with aqueous magnesium hydroxide, can be carried out at a distant source of CO2 emissions, such as a power station or on board a ship. Moreover, compared with magnesium silicate or the reaction mixture, magnesium hydroxide, having a lower molar mass and being able to react more completely with CO2, has a much higher CO2 sequestration capacity, namely tonnes of CO2 stored per tonne of magnesium hydroxide that is carbonated; this means that less material needs to transported and used to sequester the same mass of CO2 and, therefore, less energy and cost is expended in transport and handling tasks. In a non-inventive alternative embodiment, in which magnesium hydroxide powder is replaced with magnesium silicate powder in water slurry, it is surprisingly found, pursuant to the present disclosure, that it is also possible to achieve substantial direct aqueous-phase carbonation of Serpentine and Olivine powders, and substantial scrubbing of CO2 from ambient pressure flue gas. The prior art teaches that substantial and direct carbonation of Serpentine or Olivine powders is only possible under energy-intensive and costly conditions of elevated temperature or pressure, or with intense pre-processing, or with chemical additives. Pursuant to the present disclosure, it is found that high efficiency and low-cost non-inventive direct carbonation of Serpentine and Olivine can be achieved at ambient pressures and temperatures with only water or seawater and CO2 as additives in a simple carbonation reactor system. The CO2 can be pure or dilute, as in flue-gas or even in air, and at any partial pressure or temperature. In an embodiment of the present disclosure, there is injected simulated flue gas, namely a mixture of CO2 and N2, into a circulating slurry of the mineral powder in water and also in seawater. Many alternative gas-liquid mixing arrangements are possible, such as spraying of droplets solution of slurry into the gas. Similarly, many non-inventive alternative arrangements for solids-liquid mixing are possible, such as a fixed or stirred bed, or column of mineral particles through which water or brine is circulated to dissolve the mineral. By controlling a rate at which CO2 and/or mineral and/or water and/or energy are added or removed to/from the system, it was surprisingly found that conditions can be maintained in which the magnesium silicate mineral continuously dissolves and the CO2 is continuously scrubbed from the gas. Measurements of water containing Serpentine powder demonstrate an alkaline pH above pH8, and even above pH9. Serpentine and Olivine and other related magnesium silicate minerals such as chrysotile, lizardite, antigorite, and forsterite are composed of alternating crystal layers of magnesium oxide/hydroxide and silica. It is believed that the mechanism by which the magnesium silicate mineral dissolution and carbonation is possible under such mild conditions is that a suitable pH in the range of pH 8 to pH 9 is maintained by the addition of CO2, such that successive crystal layers of magnesium hydroxide dissolve directly into solution to form a solution of magnesium bicarbonate. In this pH range, carbonate ion concentration in solution is orders or magnitude lower than bicarbonate ion concentration and the formation of passivating solid magnesium carbonate phases on the surface of magnesium silicate particles is therefore avoided. Dissolution of the magnesium oxide layers is likely to destabilise the successive silica layers in the magnesium silicate crystal, so that the silica dissolves or precipitates as a solid, possibly accelerated by surface attrition due to stirring or solution circulation. The advantages pertaining to this surprising beneficial result of being able to carbonate magnesium silicate mineral powders according to a non-inventive process, namely without any pre-processing other than mining and crushing operations, directly under ambient conditions with just water and dilute CO2 are several, namely:\| (i) magnesium silicate mineral powders are much cheaper as feedstocks for carbonation than magnesium hydroxide, or thermally or chemically activated magnesium silicate mineral powers;\| (ii) carbonation can potentially be carried out directly at a huge scale at the site of the magnesium silicate mineral deposit using the CO2 available in air, or CO2 piped to the site, and with recirculation of water no additional water supply is needed;\| (iii) recovery and separation of pure CO2 gas and pure solid magnesium carbonate from the bicarbonate solution by conventional ageing, thermal or pressure-swing processes can provide compatibility with other CO2 transport, storage or utilisation options;\| (iv) separation of pure solid magnesium carbonate from bicarbonate solution provides a saleable chemical and industrial feedstock for other processes;\| (v) separation of silica solids from the dissolution/disintegration of the magnesium silicate mineral provides a further saleable industrial feedstock; and\| (vi) Nickel and Iron and other minor elemental constituents typically present in magnesium silicate minerals and wastes may be released in the process and can potentially be economically recovered from solution or by purification of the solid products.\|[0063] The efficiency of this entire process as illustrated in FIG. 1 and FIG.2 has been analysed through various scalability experiments, wherein it has been found that, for the Magnesium-mineral Silicates, the alkaline treatment is attractive as the associated Carbonation reaction is chemically favourable at a higher pH resulting in a higher reaction rate:\| Mg2SiO4 + 2NaOH +H2O => 2Mg(OH)2 (↓) +Na2SiO3 (aqueous) (8)\| Mg(OH)2 + CO2 => MgCO3 (↓) + H2O (9)\|[0064] In one of the embodiments, it is feasible to convert Dunite, an ultramafic rock rich in Magnesium-bearing minerals, into Magnesium Hydroxide (Mg(OH)2) by using highly concentrated Sodium Hydroxide (NaOH) aqueous solutions. The effect of the reaction time and the Sodium Hydroxide (NaOH) solution concentration on the process were studied to determine optimal conditions for achieving higher rate of conversion of Magnesium-mineral Silicates into Magnesium Hydroxide (Mg(OH)2). The product phases were identified by XRD and TG analysis. Careful quantification of Forsterite and Brucite both in raw materials and products were performed using Rietveld Refinement QPA and TG. The experimental results have been illustrated in the FIG. 3a and 3b FIG. 4a and 4b, FIG. 5, FIG. 6, Fig. 7a and 7b, FIG. 8, FIG. 9, FIG. 10, FIG. 11a and 11b; these results are indicated by 300, 301, 400, 401, 500, 600,700, 701, 800, 900, 1000, 1100, 1101 respectively. The experimental results of these drawings have been briefly elucidated in the foregoing.\|[0065] The tests conducted have shown that Magnesium-mineral Silicates constituting Dunite can be almost completely substituted with Brucite in highly concentrated solutions of Sodium Hydroxide (NaOH) and heated to a temperature of substantially 180 °C. According to the experimental results, increasing the Sodium Hydroxide (NaOH) concentration and the time of reaction are both factors that positively affect the conversion of Magnesium-Silicates into Magnesium Hydroxide. A greater amount of Magnesium Hydroxide (Mg(OH)2) was produced by using either a solution of Sodium Hydroxide (NaOH) having a molar concentration of 50 mol/kg for a temporal duration of 6 hours (73 wt%), or by using a solution of Sodium Hydroxide (NaOH) having a molar concentration of 40 mol/kg for a temporal duration of 18 and 24 hours (79 - 80 wt%). The TGA analyses results were found to be in accordance with the qualitative XRD results and with the Rietveld Refinement Quantitative Phase Analysis.\|[0066] During our exploration of optimal experimental conditions for different embodiments of the Olivine-NaOH reaction, we have discovered that it is possible to achieve substantial conversion of Olivine to Brucite in open vessels at ambient atmospheric pressure while heating to temperatures in the range 130-220 °C. At these elevated temperatures the vapour pressure of water significantly exceeds the reaction pressure. This discovery provides a significant advantage over the processes described by prior art systems in that the reaction can be conducted at much lower pressures (and even at ambient atmospheric pressure) using standard low-cost industrial reactors that typically are designed to withstand operating pressures up to 10 Bar.\|[0067] In accordance with another embodiment of the present invention, compacted Dunite powder can be heated in a sealed vessel at a temperature around 180°C, preferably for around six hours, to produce a product comprising Brucite.\|[0068] In accordance with another embodiment of the present invention, the Olivine and/or Serpentine is a Magnesium mineral which are suitable feedstock materials due to their high content of Magnesium (Mg) and wide abundance and large concentration in mineralogical sites.\|[0069] From the above description and claimed process, it will be appreciated that there is provided an improved process of alkali digestion for mineral Carbonation. The process can find utility in sequestration of Carbon Dioxide (CO2), extraction of valuable minerals, and other processes, known to the person skilled in the art, requiring the digestion of minerals for their Carbonation.\|[0070] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) comprises:\| reacting an alkaline earth silicate-based material with an alkali metal compound to form a mixture comprising a hydroxide of the alkaline earth, wherein the alkali metal is selected from sodium and/or potassium, and wherein the alkaline earth is selected from magnesium and/or calcium;\| reacting the mixture at a temperature in the range 140-220 °C and at a pressure of less than 10 Bar;\| separating the hydroxide of the alkaline earth from the mixture; and\| combining the hydroxide of the alkaline earth with a source of Carbon dioxide (CO2) producing a Carbonate or Bicarbonate or the alkaline earth. This gives a very beneficial production and sequestration of the hydroxide of the alkaline earth.\|[0071] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above further includes reacting the mixture in (b) at a pressure of less than the vapour pressure of pure water at the temperature of reaction.\|[0072] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above further includes using the mixture with a stoichiometric ratio between the Si in the alkaline earth silicate-based material and the alkali metal in the alkaline compound in a range of 1:1 to 1:2.\|[0073] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes using the mixture in a form of an aqueous solution with the molality of >30 molar of alkaline compound per litre water (H2O).\|[0074] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes reacting the mixture at ambient atmospheric pressure.\|[0075] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes executing the reaction at a temperature of ca 180 °C.\|[0076] Optionally, a non-inventive method of sequestration Carbon Dioxide (CO2) as outlined above includes using flue gases with less than 50vol% Carbon Dioxide (CO2) as part of a gas mixture for carbonation.\|[0077] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes carrying out reactions in an unpressurised continuous mode to achieve substantially complete carbonation of the Magnesium Hydroxide or Magnesium silicate.\|[0078] Optionally, a non-inventive system for sequestrating Carbon Dioxide (CO2), wherein the system includes a first reaction chamber which is operable to receive a Silicate-based material and an alkaline compound, and a blending apparatus for blending contents of the first reaction chamber to produce a mixture therein.\|[0079] Optionally, the non-inventive system for sequestrating Carbon Dioxide (CO2) as described above is operable to execute the method outlined above method of sequestrating Carbon Dioxide (CO2).\|[0080] Modifications to embodiments of the invention described in the foregoing are possible without departing from the scope of the invention as defined by the accompanying claims. For example the compound in the reaction may be selected from any one or combination of Hydroxide, Carbonate, and/or Bicarbonate as would be suitable to the person skilled in the art. Expressions such as "including", "comprising", "incorporating", "consisting of", "have", "is used to describe and claim the present invention are intended to be construed in a non-exclusive manner, namely allowing for items, components or elements not explicitly described also to be present. Reference to the singular is also to be construed to relate to the plural. Numerals included within parentheses in the accompanying claims are intended to assist understanding of the claims and should not be construed in any way to limit subject matter claimed by these claims.	(EP3129125)\|TECHNICAL FIELD\|[0001] The present disclosure relates to methods of producing activated mineral silicate for use in sequestrating Carbon Dioxide, for example from flue-gas, by utilizing a process which involves digestion of metal mineral Silicates. Moreover, the present disclosure also relates to systems for executing aforesaid methods.\|BACKGROUND\|[0002] Increasing concentrations of Carbon Dioxide (CO2) in the Earth's atmosphere have recently caused concerns, as the present concentrations are substantial at 400 p.p.m. and increasing at a rate of 4 p.p.m. per annum. A major factor contributing to such increase is the anthropogenic oxidation of carbonaceous fossil fuels, for example coal, oil and gas. The World presently consumes circa 100 million barrels of oil per day.\|[0003] There have been recent initiatives to employ more renewable energy systems, for example wind turbines and tidal power generating systems, as well as sequestration of Carbon Dioxide (CO2) from flue-gases emitted from coal burning electricity generating facilities. Thus, primary initiatives involve utilizing energy efficient technologies, increasing reliance on renewable sources, and developing technologies for long term storage of Carbon Dioxide (CO2) emissions. The latter technology field is known as Carbon Dioxide (CO2) sequestration.\|[0004] There have been significant developments in Carbon Dioxide (CO2) sequestration in recent years, and Carbon Dioxide sequestration technologies have aroused considerable interest among governments, industries and scientific communities. Earlier methods of Carbon Dioxide (CO2) sequestration suffered from various drawbacks such as risk of water contamination, and a lack of suitable storage spaces for receiving sequestrated Carbon Dioxide (CO2); these drawbacks are familiar to a person skilled in the art.\|[0005] There has been considerable interest in mineral Carbonation technologies to address aforementioned problems associated with known Carbon Dioxide (CO2) sequestration. The Masters thesis by Mabell Delgado Torróntegui at ETH in Switzerland, "Assessing the Mineral carbonation science and technology" (2010), provides an overview of contemporary research in this field of Carbon Dioxide (CO2) sequestration technology. A key principle of mineral Carbonation is also known as "mineral sequestration technology", wherein sequestration of Carbon Dioxide (CO2) is achieved by capturing Carbon Dioxide (CO2) in a form of stable mineral Carbonates. Such sequestration employs a process which is an exothermic reaction of a metal Oxide and Carbon Dioxide (CO2) to form stable Carbonate materials as provided in a reaction formula (1):\| MO + CO2 => MCO3 + Heat (1)\|wherein M is a metal, preferably an alkaline earth metal such as Calcium or Magnesium.\|[0006] Most suitable and naturally abundant sources of these metal Oxides are Magnesium or Calcium Silicate minerals such as Olivine, wollastonite, and Serpentine. The Carbonation reactions of these minerals are as follows:\| Olivine:\| Mg2SiO4 + 2CO2 => 2MgCO3 + SiO2 + 89 kJ mol-1CO2 (2)\| Serpentine:\| Mg3Si2O3(OH)4 + 3CO2 => 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol-1CO2\| Wollastonite:\| CaSiO3 + CO2 => CaCO3 + SiO2 + 90 kJ mol-1CO2 (4)\|[0007] Although the above reactions (2) to (4) are thermodynamically favourable, the reactions in nature have, however, relatively slow reaction rates in a geologic time scale, and are unsuitable for industrial processes. Efforts have been made to try to accelerate these reactions. However, the efforts suffer from various limitations, such as energy wastage and a high cost of mining and transporting large amounts of rock, as well as industrial and environmental inefficiencies. Moreover, the mineral Silicates are not easily obtainable in suitable quantities and formats for allowing satisfactory mineral Carbonation to be achieved.\|[0008] In a published US patent no. US7604787B2 (MAROTO-VALER), "Process for sequestering Carbon Dioxide and Sulphur Dioxide", there is described a method of reacting a Silicate-based material with an acid to form a suspension, which is then combined with Carbon Dioxide to produce a metal salt, silica and regenerating acid in solution. This method has drawbacks of being environmentally harsh and inefficient. Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for removal and Capture of Carbon Dioxide from Flue Gases".\|[0009] Although, the prior art disclosures have been able to address some of the problems of mineral Carbonation through their indirect sequestration processes, there are several remaining problems which have not yet been resolved. Such remaining problems pertain to industrial scalability, environmental efficiency, and cost.\|[0010] Lately, research effort has focused upon Carbon Dioxide (CO2) sequestration by 'direct' Carbonation of Olivine or Serpentine. In these recent methods, Carbon Dioxide (CO2) is sequestered without acid pretreatment of Silicate feedstock. An Olivine reaction is:\| Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 (5)\|[0011] Moreover, for Serpentine, a corresponding reaction is:\| Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O (6)\|[0012] Experiments to determine the kinetics of these reactions (5) and (6) have shown that such reactions also suffer from poor energy efficiency and a high cost when up-scaled to an industrial plant. In order to accelerate the reactions (5) and (6), high temperatures in a range of 600°C to 650 °C are required. In a fuel-fired industrial power plant, attainment of such high temperatures would translate to a requirement of approximately 200 kW-h of electricity per tonne of Serpentine feedstock. Moreover, with a fossil fuel containing 1 tonne of Carbon, nearly 3.7 tonnes of Carbon Dioxide (CO2) is produced. Each tonne of Carbon Dioxide (CO2) consumes more than 2 tonnes of Serpentine during Carbonation. Combined with a pre-capture step to separate and pressurise CO2 from flue gas, the power required for Serpentine dehydroxylation Is around 20-30% of total power output from such fuel-fired industrial power plant. All these considerations lead to a huge energy penalty threatening the economic feasibility of this sequestration process.\|[0013] In a published US patent no. US8114374B2 (BLENCOE), "Carbonation of metal Silicates for long-term CO2 sequestration", there is described a method (hereinafter "Blencoe's method") of reacting a Silicate with an alkali metal hydroxide in an aqueous solution. The reaction with Carbon Dioxide (CO2) is then used to carbonate the metal formerly contained in the metal Silicate. This method has drawbacks of inefficiencies and poor overall Carbon capture properties. Blencoe's method comprises three steps:\| (1) reacting a metal silicate with a caustic alkali-metal hydroxide to produce a hydroxide of the metal formerly contained in the silicate;\| (2) reacting carbon dioxide with at least one of a caustic alkali-metal hydroxide and an alkali-metal silicate to produce at least one of an alkali-metal carbonate and an alkali-metal bicarbonate; and\| (3) reacting the metal hydroxide product of step (a) with at least one of the alkali-metal carbonate and the alkali-metal bicarbonate produced in step (b) to produce a carbonate of the metal formerly contained in the metal silicate of step (a).\|[0014] In Blencoe's first step (1), the alkali-metal hydroxide is in aqueous solution which limits the maximum reaction temperature to the vapour pressure of the aqueous solution at the pressure under which the reaction is carried out. A low reaction temperature limits the reaction rate at atmospheric pressure, while use of a pressurised vessel increases process costs. Alkali-metal hydroxides, such as NaOH and KOH, used in steps (1) and (2) are energy intensive and expensive chemicals to manufacture. In Blencoe's second step (1), alkali-metal hydroxide, additional to that used in step (1), is used to react with Carbon Dioxide. In Blencoe's second and third steps (2) and (3), an elevated pressure is required, namely having implied costs of a pressure vessel, in the range between the vapour pressure of water at the reaction temperature and Bar. It is doubtful that the overall process described is able to sequester more Carbon Dioxide as a metal carbonate than is generated as a consequence of manufacture of the alkali-metal hydroxides consumed in the process, or that the process is any cheaper to operate than Carbon Dioxide sequestration processes described in the prior art.\|[0015] Therefore, there is an urgent need to develop a process which is energy efficient, has a high throughput and is more cost effective than the prior art so that it can be used industrially.\|[0016] From the foregoing, it will be appreciated that the known methods of processing and the systems for mineral carbonation and Carbon Dioxide (CO2) sequestration, are neither optimal in their manner of operation nor adaptable to broader applications in a cost effective manner.\|SUMMARY\|[0017] The present invention seeks to provide an improved method of activation of magnesium silicate minerals by conversion to magnesium hydroxide.\|[0018] This present embodiment of the invention allows for a method of large scale industrial use and continuous carbonation without advanced pressure chambers or equipment.\|[0019] The present invention provides a method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, wherein the method comprises:\| a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from a group comprising alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture;\| b. heating the dry solid-solid mixture to a temperature below 300°C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and\| c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|[0020] Optionally, the method includes the liquid slurry of step c being separated into solid and aqueous solution phase products.\|[0021] Optionally, the method includes reacting any of the aqueous phases at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|[0022] Optionally, the method includes mixing the solid phase product with water and reacted at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|[0023] Optionally, the method includes air or flue gas as the gas in the reaction. This allows for a very simple and cost-effective solution utilizing what is available at the site of operation.\|[0024] Optionally, the method includes using a hydroxide or a carbonate of sodium or a potassium as the alkali metal compound in the reaction.\|[0025] Optionally, the method includes a serpentine or an olivine rock as the magnesium silicate mineral in the reaction. Further, optionally, the method includes heating the unpressurised vessel in step (b) to a temperature in the range 140 °C - 220 °C.\|[0026] Optionally, the method includes continuously adding the magnesium silicate mineral and alkali metal compound of step (a) together allowing continuous reacting thereof under the conditions of step (b) and further continuously removing the product of step (b).\|[0027] Optionally, the method includes the molar ratio of substantially 2 moles of alkali metal per mole of silicon in the mixture.\|[0028] Additional aspects, advantages, features and objects of the present invention would be made apparent from the drawings and the detailed description of the illustrative embodiments construed in conjunction with the appended claims that follow. It will be appreciated that features of the present invention are susceptible to being combined in various combinations from different embodiments without departing from the scope of the present invention as defined by the appended claims.\|DESCRIPTION OF DRAWINGS:\|[0029] The summary above, as well as the following detailed description of illustrative embodiments, is better understood when read in conjunction with the appended drawings. For the purpose of illustrating the present invention, exemplary constructions of the disclosure are shown in the drawings. However, the present invention is not limited to specific methods and apparatus disclosed herein. Moreover, those in the art will understand that the drawings are not to scale. Wherever possible, like elements have been indicated by identical numbers.\| FIG. 1 is an illustration of a flow chart of a digestion Step 1 involving alkaline digestion of Serpentine or Olivine to convert them to Brucite and Silica;\| FIG. 2 is an illustration of a flow chart of a Carbonation step 2 involving direct Carbonation of Brucite, namely Magnesium Hydroxide, with flue-gas to form Magnesium Carbonate;\| FIG.3a and 3b are illustrations of XRD patterns of selected samples, wherein solid products from dissolution of Dunite, namely a form of Olivine, using Sodium Hydroxide (NaOH) solution of concentration in a range of 15 to 40 mol/kg (left), and using Sodium Hydroxide (NaOH) solution of concentration 50 mol/kg (right) solutions. In the illustrations, following abbreviations are employed: Fo = Forsterite, Brc = Brucite, Clc = Clinochlore, En = Enstatite, Srp = Serpentine, Tlc = Talc, Spl = Spinel;\| FIG. 4a and 4b are illustrations of TG (4a) and DTG (4b) curves of selected samples: solid products from dissolution of Dunite at a temperature of 180°C for 15 for 6 hours with different concentrations of Sodium Hydroxide (NaOH) solution;\| FIG. 5 is a graph wherein there are shown Mg(OH)2 concentrations in solid products based on TG results: Dunite dissolved at a temperature of 180°C with different concentrations of Sodium Hydroxide (NaOH) solution, namely measured as moles of NaOH per kg of water. From the graph, it will be appreciated that the proportion of Dunite, namely magnesium silicate, converted to Brucite, namely magnesium hydroxide, increases approximately linearly with increase in NaOH concentration; extrapolation of this graph indicates that the proportion of Brucite in the solid product should approach 100% above a NaOH concentration >70mol/kg, namely equivalent to a NaOH: H2O ratio >1.26;\| FIG. 6 is an illustration of XRD patterns of solid products from dissolution of Dunite at 180 °C with Sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg solution, for different temporal durations;\| FIG. 7a and 7b are illustrations of TG (7a) and DTG (7b) curves of solid products from dissolution of Dunite at a temperature of 180° C with sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg for different temporal durations;\| FIG. 8 is a graph in which there is shown Magnesium Hydroxide Mg(OH)2 concentration in solid products based on TG results: Dunite dissolved at a temperature of 180 °C with a molar concentration of Sodium Hydroxide (NaOH) solution being 40 mol/kg for different durations;\| FIG. 9 is an illustration showing Rietveld Refinement QPA of raw Dunite, wherein: data points profile = experimental pattern; continue profile = calculated model (above); difference plot (below);\| FIG. 10 is an illustration showing Rietveld Refinement QPA of dissolved Dunite spiked with 10 wt% Silicon, wherein: data points profile = experimental pattern; continue profile = calculated model; and\| FIG. 11a and 11b are illustrations showing Brucite quantification with Rietveld Refinement and TGA (FIG. 11a), wherein Forsterite and Brucite concentrations were obtained via Rietveld Refinement QPA of selected samples (FIG. 11b).\| FIG. 12a and 12b depict experimental data concerning the removal of CO2 by means of Brucite powder in aqueous suspension, specifically the resulting CO2 level for a monitored exit gas after processing.\|[0030] In the accompanying drawings, an underlined number is employed to represent an item over which the underlined number is positioned or an item to which the underlined number is adjacent. A non-underlined number relates to an item identified by a line linking the non-underlined number to the item. When a number is non-underlined and accompanied by an associated arrow, the non-underlined number is used to identify a general item at which the arrow is pointing.\|DETAILED DESCRIPTION OF EMBODIMENTS\|[0031] The following detailed description illustrates embodiments of the present disclosure and ways in which they can be implemented.\|[0032] In FIG. 1, there is shown a digestion process 100, wherein there occurs alkaline digestion of a Silicate-based material, a naturally occurring feedstock containing magnesium or calcium silicate, such as Serpentine, Olivine, Dunite, and/or Wollastonite 101. The process 100 results in reaction products being generated, namely a conversion to Brucite and Silica in a case of Olivine 101 being a feed mineral employed. In the reaction, Olivine 101 is fed into a stirred reactor 102 together with an alkali 103 and heat is provided from a heat source 104. The alkali is beneficially selected from a mineral Hydroxide. Among the many metal Hydroxides that can find utility in this reaction, a preferable alkali used is Sodium Hydroxide (NaOH) .\|[0033] The reaction mixture of the digestion process 100 comprises a stoichiometric ratio between the soluble silicate based material and the solid hydroxide of the alkaline earth compound of about 1:2. This stoichiometric ratio aims to minimise the input of the alkaline compound, such as Sodium Hydroxide (NAOH), into the initial reaction mixture. This limits the regeneration of Sodium Hydroxide (NaOH) from carbonates at the end of the reaction, which is costly and time consuming. The reaction mixture is a dry mixture.\|[0034] According to a further embodiment, the reaction mixture is a solid-state dry mixture of a powder of the alkaline-earth silicate and the alkali-metal compound, in the stoichiometric ratio of one mole of silicon, namely in the silicate, per two moles of alkali-metal. Solid alkali-metal compounds, such as NaOH, KOH and Na2CO3, have high melting points, namely 318°C, 406°C and 851 °C, respectively. Using an aqueous system, such as taught by Blencoe, would therefore be expected to be essential to achieving mixing and reaction at temperatures below 300 °C. Surprisingly, in experiments using NaOH and Serpentine, namely magnesium silicate, it is found that a dry solid state mixture of the two rapidly melted, mixed and reacted to form magnesium hydroxide in an unpressurised vessel at temperatures as low as 180°C, namely well below the melting temperature of NaOH, namely 318°C, or of Serpentine, namely >1700 °C. Unlike Olivine, Serpentine has a crystal structure that contains chemically bound hydroxide groups, and it is believed that these groups may facilitate the dry stoichiometric reaction to form magnesium hydroxide.\|[0035] Dunite can also be used to yield Mg(OH)2 via solid state reaction, with a preferable ratio of Dunite to NaOH in a mole ratio of 1:2, at a temperature around 180 °C. Experiments conducted with a range of Dunite: NaOH mole ratios of 1:0.5, 1:1, 1:.5 and 1:2, where the powder has been formed into pellets by compaction with a hand press (3 tonnes for 1 minute for compression), returned results indicating a linear increase of Mg(OH)2 production with increase of NaOH, to a maximum weight percentage of Mg(OH)2 in the reaction products of around 46.7%. Reducing the amount of NaOH significantly lowered the extraction efficiency of the process.\|[0036] In contrast, results of non-inventive experiments, as provided in FIGs. 3a, 3b, 5, with aqueous NaOH and Olivine show that minimum reaction conditions of a temperature of 180°C and a NaOH concentration of 40mol/kg are substantially required to form magnesium hydroxide; this system requires a pressure vessel to reach a required reaction temperature.\|[0037] For the case of Dunite samples, comparison of the results cited above with alkaline digestion of Dunite with 50mol/kg NaOH aqueous system at 180°C under a similar time period, show that the yield of Mg(OH)2 via solid state reaction (55% to 62%) was on a par with that produced using the aqueous system (between 58% and 66%). The alkaline digestion with 50mol/kg NaOH required significantly more NaOH per 1 gram of Dunite processed such that the solid state reaction effected a 97% to 99% reduction of NaOH consumption. Additional experimental results comprising Dunite as a sample component are detailed later.\|[0038] Generally stated, it has been demonstrated that it is possible to extract Mg(OH)2 from magnesium containing silicate minerals via solid state reaction with NaOH and that the consumption of the alkaline reactant can be reduced, achieving significant yield of reaction. An additional advantage is the reduction of water consumption which would be needed for an aqueous process.\|[0039] Moreover, results have also shown, namely in FIG. 5, that without water, the NaOH concentration (mol/kg) effectively approaches infinity and might therefore be expected to approach 100% conversion of magnesium silicate to magnesium hydroxide. Compared to the aqueous reaction system, as exemplified by Blencoe, clear benefits of the non-aqueous dry-mixture and stoichiometric system using Serpentine are that:\| (i) no pressure vessel is required;\| (ii) melting and mixing surprisingly take place at 180 °C, to enable a rapid reaction at a rate similar to an aqueous system;\| (iii) a highest possible concentration and activity of NaOH is enabled, leading to a faster and more complete reaction than possible in an aqueous system at a similar temperature;\| (iv) the NaOH is totally consumed in a reaction with silicate to form solid sodium silicate, so that no subsequent process for recovery of excess NaOH from the reaction products is required;\| (v) Serpentine provides any water required for the stoichiometric conversion to magnesium hydroxide from its structural hydroxide groups, so that no free water needs to be added to the reaction system;\| (vi) the products of reaction, containing no excess NaOH, are a solidified glass which is substantially less caustic than in the aqueous process and are therefore much safer to handle;\| (vii) sodium silicate is readily separated from the products of reaction by dissolution and filtration, and is available without contamination by NaOH; and\| (viii) the process can be more readily and cheaply carried out at remote Serpentine or Olivine mine sites where water may not be available.\|[0040] Further, in the prior art of Blencoe it is described how the initial step (a) can be conducted at a pressure slightly below the vapour pressure of pure water for the temperature of that step. Blencoe does not claim a preferred temperature or pressure or aqueous solution composition for that initial step (a), but in a table of experimental results shows that all reactions in which serpentine or olivine are converted to a major phase of brucite are done in aqueous solution in a pressure vessel at a temperature of 200 °C and pressure <15atm. One experiment conducted at a temperature of 22 °C and 1atm pressure for 72hrs results in conversion to a minor phase of brucite; subsequent additional reaction at 200 °C and < 15bar then converts substantially to brucite with a minor residual phase of serpentine. Notwithstanding Blencoe's assertion of the technological and commercial advantage of avoiding pressure-intensifying equipment, at the effective reaction temperature of 200 °C for Blencoe's step (a), the vapour pressure of pure water is just above bar indicating that a pressure vessel must be used in this step. The current invention allows for the method and system to operate without expensive and complicated equipment used in Blencoe to operate at higher than atmospheric pressure.\|[0041] In the example of magnesium carbonates being produced according to the described method, a wide range of compounds including soluble magnesium bicarbonate Mg(HCO3)2 is produced in solution, but generates no separate water in the carbonation reaction:\| 2CO2+ Mg(OH)2 = Mg.(HCO3)2 (7)\|[0042] The preferred alkali 103 for this digestion process is beneficially Sodium Hydroxide or Potassium Hydroxide. It is also possible to use Sodium Carbonate, Sodium Bicarbonate, Potassium Carbonate and Potassium Bicarbonate as the alkali for the digestion process.\|[0043] The heat source 104 is employed to raise a temperature of the digestion process, whilst stirring of the mixture is implemented, to a temperature of less than 250 °C, and for a temporal period of less than 6 hours. A preferred range of temperature is from 140 °C to 220 °C. The reaction can be best performed with the temperature being less than 200 °C, and most preferentially at around 180 °C, throughout the process, as shown in the results FIG. 4 to FIG. 8. The digestion vessels used are most suitably Teflon (PTEE) to withstand hot-conc-NaOH with the maximum operating temperature usually specified at 220 °C. Experiments with Magnesium silicate mineral feedstocks have been showing excellent results for this process.\|[0044] This digestion process is preferably carried out at a pressure of less than Bar, wherein 1 Bar corresponds to nominal atmospheric pressure at sea-level. The reaction can be more preferably carried out at a pressure less than 10 Bar. The reaction can be furthermore preferably be carried out at pressure conditions lower than the vapour pressure of pure water at the temperature of reaction. The benefit of not having to use high pressure vessels to carry out hydrothermal reactions saves cost and also improves the applications of the technology in industrial applications at very high volumes and large scale installations.\|[0045] The process, after digestion of Olivine, is shown in equation 112. Here, the Brucite (MgOH2) 107, solid phase, is separated from a Silicate solution 108. Thereafter, the Silica precipitation process is carried out as depicted in the equations 113 and 112. The process, namely acid precipitation, can be carried out by adding either Carbon Dioxide (CO2) or acid 110. Excess alkali 111 is recovered and fed back to a chamber of the reactor 102. Performing the digestion process at ambient atmospheric pressure conditions avoids a need to employ equipment to increase pressure, for example an autoclave, and allows large scale, continuous sequestration of industrial Carbon Dioxide (CO2) emissions to be achieved. Avoiding the requirement for any pressurised containment of the reaction steps, provides several benefits:\| (i) much cheaper and simpler reaction vessels can be used;\| (ii) it is easier and cheaper to incorporate mixing, stirring and/or particle attrition to enhance reaction rates within an unpressurised reaction vessel;\| (iii) energy usage, namely energy wasted in pressurisation/ depressurisation, is lower;\| (iv) product throughput is faster, namely a need for time to pressurise is avoided; and\| (v) while pressurised reaction systems tend to operate in batch mode, it is much easier to configure each step, and also the overall process, as a continuous operation in an unpressurised system.\|[0046] Continuous operation is generally recognised by process engineers as preferable to batch operations because:\| (a) reaction parameters such as temperature, pH and reactant concentrations are easier to maintain at fixed optimum levels; and\| (b) residence times are shorter, thereby enabling process equipment to be smaller and cheaper and product throughput higher.\|[0047] In FIG. 2, there is provided an illustration of the details of a Carbonation process 200 as also depicted in equations 206 and 207. The Brucite (MgOH2) powder 205 is fed into a continuous reactor 201, together with a flue-gas 204. The de-carbonised flue gas 202 and Magnesium Carbonate (MgCO3) powder 203 are the reaction products of this Carbonation process 200.\|[0048] In a further embodiment of the present invention, Mg(OH)2 (Brucite) powder is provided as added to water to form an aqueous suspension which is then used at ambient temperature and pressure to scrub CO2 from a gaseous mixture of nitrogen (N2) and CO2.The scrubbing process using wet-Brucite which simultaneously removes the CO2 from the gas mixture and converts the Brucite to magnesium carbonates. Substantial removal and conversion can be achieved such that most, if not all, of the CO2 is taken out of the gas mixture and most, if not all, of the Brucite is converted.\|[0049] Following a particular example of such a further embodiment of the invention, consider the following experiment:\|A gas mixture of (nitrogen) N2 containing 4-5% CO2 (carbon dioxide, cylinder pre-mix) was bubbled continuously at a fixed flow-rate (around 2.25 litres/minute) through a fixed circulating volume (around 10 litres) of water (pre-saturated before the experiment with 5%CO-N2) containing a suspension of magnesium hydroxide powder (0.871 mol, 50.8 grams). The CO2 concentration in the exit gas was initially zero (as it was totally removed by reaction with Brucite) and was monitored as the suspended Brucite particles were consumed in the reaction to form dissolved magnesium bicarbonate. Periodic samples of the circulating liquid were taken to monitor change in pH and magnesium ion concentration. The experiment was concluded when the concentration of CO2 in the exit gas had increased to equal that of the inlet concentration, indicating that no further reaction was occurring. The experiment took approximately 12 hours to complete and was run over the course of two days with an overnight shut-down.\|[0050] A Down-flow Gas Contactor (DGC, WRK Design & Services Ltd) with a liquid volume of around 10 litres was used as the gas-liquid reactor. In this reactor, the gas-mixture at atmospheric pressure entered at the top of a bubble column, entrained in a downward circulating liquid flow. The rate of liquid recirculation in the DGC reactor (around 10 litres/min) was adjusted to maintain a stable bubble-liquid interface. The CO2-depleted gas exited from the bottom of the column after reaction and separation from the recirculating liquid phase. Gas flow rate was measured by calibrated glass tube rotammeter at a fixed 2.25 litres/minute (atmospheric pressure).\|[0051] Concentration of CO2 was measured using a calibrated inline infrared datalogger (range: 0-5 % CO2 measured to nearest 0.25 %). Temperature was ambient, in a range of 9.5-11 °C. Solution pH was in a range of pH 8.2-8.9.\|[0052] The DGC reactor provides a large and dynamic interfacial area between gas bubbles and circulating liquid. During the course of the experiment, CO2 dissolves from the gas (g) into the liquid (I) phase (or aqueous phase, aq) and reactions occur with the suspended Brucite particles (solid phase being labelled as s):\| CO2 (g) = CO2 (aq) (E1)\| CO2 (aq) + H2O(I) = H2CO3 (aq) (E2)\| H2CO3 (aq) = H+(aq) + HCO3-(aq) (E3)\| HCO3-(aq) = H+(aq) + CO32-(aq) (E4)\| Mg(OH)2(s) = Mg2+(aq) + 2OH-(aq) (E5)\| Mg(OH)2(s) + CO2(aq) = MgCO3(s) + H2O(I) (E6)\| Mg(OH)2(s) + 2CO2(aq) = Mg2+(aq) + 2HCO3-(aq) (E7)\| Mg2 +(aq) + CO32-(aq) = MgCO3(s) (E8)\| MgCO3(s) + CO2(aq) = Mg2+(aq) + 2HCO3-(aq) (E9)\|[0053] In alkaline solution, Brucite solubility is well known to be negligible while CO2 dissolves readily. In the pH range of the experiment, pH falls in the range 8.2-8.9, the predominant form of carbon in solution is the bicarbonate ion, HCO3- (aq). The dominant reactions in this situation may therefore be expected to be:\| CO2 (g) + H2O(I) = H+(aq) + HCO3-(aq) (E10)\|and\| Mg(OH)2(s) + 2H+(aq) = Mg2+(aq) + 2H2O(I) (E11)\|[0054] At higher pH, where carbonate ions dominate, the formation of solid magnesium carbonate phases would be expected and, moreover, may precipitate on the surface of the suspended Brucite particles, blocking the Brucite to further reaction with CO2.At lower pH, dissolution of CO2 would be inhibited. However, at pH 8-9, where bicarbonate ions are greatly in excess of carbonate ions, formation of solid magnesium carbonate phases should be minimal, with the result that suspended Brucite particles should fully react with CO2, ideally in a mole ration of 1:2, to form an aqueous solution of magnesium bicarbonate.\|[0055] CO2 concentrations in exit gas were data-logged continuously. Occasional measurements of (fixed) inlet CO2 concentration were taken. The resulting data is shown in the two charts: one for day 1 detailing results 1200 (Fig. 12a) and one for day 2 detailing results 1201 (Fig 12b), 5 showing CO2 concentration (%CO2) versus time.\|[0056] Analysis: The total amount of CO2 removed from the inlet gas is calculated from the measured gas flow-rate and the measured difference between inlet and outlet gas concentration: \|[0057] Uncertainty in the flow-rate measurement (rotameter) is estimated from rotameter specifications as 3 %. The CO2 meter was able only to measure to the nearest 0.5 % in a CO2 concentration range of 0-5 %. Additionally, the inlet gas CO2 concentration from the pre-mix cylinder was measured at different times in the experiment as 4 % and 5 %. Absolute uncertainty in the measured % CO2 concentration change is estimated at 0.7 % CO2.\|[0058] The total amount of CO2 removed from the inlet gas during the 12 hour course of the experiment was measured as 1.87 moles (± 0.2 moles). Within experimental error, this is the amount of CO2 expected to be removed if all 0.871 moles of the initial Brucite had reacted with CO2 to form dissolved magnesium bicarbonate according to reaction (E7) above. Within the limits of measurements errors, results show that 100 % utilisation (carbonation) of Brucite is feasible when wet-scrubbing 5 % CO2-N2 gas mixture.\|[0059] Results also show that for the first 3.5 hours of the 12 hour experimental period, removal of CO2 from the inlet 5 % CO2-N2 gas mixture was 100 %. Over the first 6 hrs (first day), CO2 removal averaged 93 % and over the full 12 hours averaged 62%. Results show unequivocally that a Brucite-water suspension can fully scrub CO2 from dilute gas mixtures.\|[0060] It may be expected that in a future industrial CO2 scrubbing system, in which the rates of water, Brucite and CO2 addition may be controlled to maintain pH within a range of around pH 8 to pH 9, and where magnesium bicarbonate is removed, continuous removal of CO2, controllable up to 100%, should be possible and/or simultaneous with up to 100% conversion of Brucite to magnesium carbonates.\|[0061] Referring to "unpressurized" mentioned in the foregoing, it is optionally feasible to vent apparatus for implementing embodiments of the present disclosure directly to ambient atmosphere, namely substantially 1 Bar pressure, thereby avoiding a need for using expensive pressure vessels. However, optionally, embodiments of the present disclosure are operated in a substantially unpressurized manner at pressures in a range of 0.5 Bar to 10.0 Bar, more optionally in a range of 0.8 Bar to 5.0 Bar, and yet more optionally in a range of 0.9 Bar to 2.0 Bar. It will be appreciated that "pressurized", in contradistinction, refers to pressures, for example, in excess of 20 Bar, in excess of 50 Bar, or even in excess of 100 Bar.\|[0062] For example, the first steps of the process in which a mined magnesium silicate mineral is converted into magnesium hydroxide can be carried out at the mine site, while, without a need for elevated temperatures or pressures for reaction, the final step in which CO2 in flue-gas reacts with aqueous magnesium hydroxide, can be carried out at a distant source of CO2 emissions, such as a power station or on board a ship. Moreover, compared with magnesium silicate or the reaction mixture, magnesium hydroxide, having a lower molar mass and being able to react more completely with CO2, has a much higher CO2 sequestration capacity, namely tonnes of CO2 stored per tonne of magnesium hydroxide that is carbonated; this means that less material needs to transported and used to sequester the same mass of CO2 and, therefore, less energy and cost is expended in transport and handling tasks. In a non-inventive alternative embodiment, in which magnesium hydroxide powder is replaced with magnesium silicate powder in water slurry, it is surprisingly found, pursuant to the present disclosure, that it is also possible to achieve substantial direct aqueous-phase carbonation of Serpentine and Olivine powders, and substantial scrubbing of CO2 from ambient pressure flue gas. The prior art teaches that substantial and direct carbonation of Serpentine or Olivine powders is only possible under energy-intensive and costly conditions of elevated temperature or pressure, or with intense pre-processing, or with chemical additives. Pursuant to the present disclosure, it is found that high efficiency and low-cost non-inventive direct carbonation of Serpentine and Olivine can be achieved at ambient pressures and temperatures with only water or seawater and CO2 as additives in a simple carbonation reactor system. The CO2 can be pure or dilute, as in flue-gas or even in air, and at any partial pressure or temperature. In an embodiment of the present disclosure, there is injected simulated flue gas, namely a mixture of CO2 and N2, into a circulating slurry of the mineral powder in water and also in seawater. Many alternative gas-liquid mixing arrangements are possible, such as spraying of droplets solution of slurry into the gas. Similarly, many non-inventive alternative arrangements for solids-liquid mixing are possible, such as a fixed or stirred bed, or column of mineral particles through which water or brine is circulated to dissolve the mineral. By controlling a rate at which CO2 and/or mineral and/or water and/or energy are added or removed to/from the system, it was surprisingly found that conditions can be maintained in which the magnesium silicate mineral continuously dissolves and the CO2 is continuously scrubbed from the gas. Measurements of water containing Serpentine powder demonstrate an alkaline pH above pH8, and even above pH9. Serpentine and Olivine and other related magnesium silicate minerals such as chrysotile, lizardite, antigorite, and forsterite are composed of alternating crystal layers of magnesium oxide/hydroxide and silica. It is believed that the mechanism by which the magnesium silicate mineral dissolution and carbonation is possible under such mild conditions is that a suitable pH in the range of pH 8 to pH 9 is maintained by the addition of CO2, such that successive crystal layers of magnesium hydroxide dissolve directly into solution to form a solution of magnesium bicarbonate. In this pH range, carbonate ion concentration in solution is orders or magnitude lower than bicarbonate ion concentration and the formation of passivating solid magnesium carbonate phases on the surface of magnesium silicate particles is therefore avoided. Dissolution of the magnesium oxide layers is likely to destabilise the successive silica layers in the magnesium silicate crystal, so that the silica dissolves or precipitates as a solid, possibly accelerated by surface attrition due to stirring or solution circulation. The advantages pertaining to this surprising beneficial result of being able to carbonate magnesium silicate mineral powders according to a non-inventive process, namely without any pre-processing other than mining and crushing operations, directly under ambient conditions with just water and dilute CO2 are several, namely:\| (i) magnesium silicate mineral powders are much cheaper as feedstocks for carbonation than magnesium hydroxide, or thermally or chemically activated magnesium silicate mineral powers;\| (ii) carbonation can potentially be carried out directly at a huge scale at the site of the magnesium silicate mineral deposit using the CO2 available in air, or CO2 piped to the site, and with recirculation of water no additional water supply is needed;\| (iii) recovery and separation of pure CO2 gas and pure solid magnesium carbonate from the bicarbonate solution by conventional ageing, thermal or pressure-swing processes can provide compatibility with other CO2 transport, storage or utilisation options;\| (iv) separation of pure solid magnesium carbonate from bicarbonate solution provides a saleable chemical and industrial feedstock for other processes;\| (v) separation of silica solids from the dissolution/disintegration of the magnesium silicate mineral provides a further saleable industrial feedstock; and\| (vi) Nickel and Iron and other minor elemental constituents typically present in magnesium silicate minerals and wastes may be released in the process and can potentially be economically recovered from solution or by purification of the solid products.\|[0063] The efficiency of this entire process as illustrated in FIG. 1 and FIG.2 has been analysed through various scalability experiments, wherein it has been found that, for the Magnesium-mineral Silicates, the alkaline treatment is attractive as the associated Carbonation reaction is chemically favourable at a higher pH resulting in a higher reaction rate:\| Mg2SiO4 + 2NaOH +H2O => 2Mg(OH)2 (↓) +Na2SiO3 (aqueous) (8)\| Mg(OH)2 + CO2 => MgCO3 (↓) + H2O (9)\|[0064] In one of the embodiments, it is feasible to convert Dunite, an ultramafic rock rich in Magnesium-bearing minerals, into Magnesium Hydroxide (Mg(OH)2) by using highly concentrated Sodium Hydroxide (NaOH) aqueous solutions. The effect of the reaction time and the Sodium Hydroxide (NaOH) solution concentration on the process were studied to determine optimal conditions for achieving higher rate of conversion of Magnesium-mineral Silicates into Magnesium Hydroxide (Mg(OH)2). The product phases were identified by XRD and TG analysis. Careful quantification of Forsterite and Brucite both in raw materials and products were performed using Rietveld Refinement QPA and TG. The experimental results have been illustrated in the FIG. 3a and 3b FIG. 4a and 4b, FIG. 5, FIG. 6, Fig. 7a and 7b, FIG. 8, FIG. 9, FIG. 10, FIG. 11a and 11b; these results are indicated by 300, 301, 400, 401, 500, 600,700, 701, 800, 900, 1000, 1100, 1101 respectively. The experimental results of these drawings have been briefly elucidated in the foregoing.\|[0065] The tests conducted have shown that Magnesium-mineral Silicates constituting Dunite can be almost completely substituted with Brucite in highly concentrated solutions of Sodium Hydroxide (NaOH) and heated to a temperature of substantially 180 °C. According to the experimental results, increasing the Sodium Hydroxide (NaOH) concentration and the time of reaction are both factors that positively affect the conversion of Magnesium-Silicates into Magnesium Hydroxide. A greater amount of Magnesium Hydroxide (Mg(OH)2) was produced by using either a solution of Sodium Hydroxide (NaOH) having a molar concentration of 50 mol/kg for a temporal duration of 6 hours (73 wt%), or by using a solution of Sodium Hydroxide (NaOH) having a molar concentration of 40 mol/kg for a temporal duration of 18 and 24 hours (79 - 80 wt%). The TGA analyses results were found to be in accordance with the qualitative XRD results and with the Rietveld Refinement Quantitative Phase Analysis.\|[0066] During our exploration of optimal experimental conditions for different embodiments of the Olivine-NaOH reaction, we have discovered that it is possible to achieve substantial conversion of Olivine to Brucite in open vessels at ambient atmospheric pressure while heating to temperatures in the range 130-220 °C. At these elevated temperatures the vapour pressure of water significantly exceeds the reaction pressure. This discovery provides a significant advantage over the processes described by prior art systems in that the reaction can be conducted at much lower pressures (and even at ambient atmospheric pressure) using standard low-cost industrial reactors that typically are designed to withstand operating pressures up to 10 Bar.\|[0067] In accordance with another embodiment of the present invention, compacted Dunite powder can be heated in a sealed vessel at a temperature around 180°C, preferably for around six hours, to produce a product comprising Brucite.\|[0068] In accordance with another embodiment of the present invention, the Olivine and/or Serpentine is a Magnesium mineral which are suitable feedstock materials due to their high content of Magnesium (Mg) and wide abundance and large concentration in mineralogical sites.\|[0069] From the above description and claimed process, it will be appreciated that there is provided an improved process of alkali digestion for mineral Carbonation. The process can find utility in sequestration of Carbon Dioxide (CO2), extraction of valuable minerals, and other processes, known to the person skilled in the art, requiring the digestion of minerals for their Carbonation.\|[0070] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) comprises:\| reacting an alkaline earth silicate-based material with an alkali metal compound to form a mixture comprising a hydroxide of the alkaline earth, wherein the alkali metal is selected from sodium and/or potassium, and wherein the alkaline earth is selected from magnesium and/or calcium;\| reacting the mixture at a temperature in the range 140-220 °C and at a pressure of less than 10 Bar;\| separating the hydroxide of the alkaline earth from the mixture; and\| combining the hydroxide of the alkaline earth with a source of Carbon dioxide (CO2) producing a Carbonate or Bicarbonate or the alkaline earth. This gives a very beneficial production and sequestration of the hydroxide of the alkaline earth.\|[0071] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above further includes reacting the mixture in (b) at a pressure of less than the vapour pressure of pure water at the temperature of reaction.\|[0072] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above further includes using the mixture with a stoichiometric ratio between the Si in the alkaline earth silicate-based material and the alkali metal in the alkaline compound in a range of 1:1 to 1:2.\|[0073] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes using the mixture in a form of an aqueous solution with the molality of >30 molar of alkaline compound per litre water (H2O).\|[0074] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes reacting the mixture at ambient atmospheric pressure.\|[0075] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes executing the reaction at a temperature of ca 180 °C.\|[0076] Optionally, a non-inventive method of sequestration Carbon Dioxide (CO2) as outlined above includes using flue gases with less than 50vol% Carbon Dioxide (CO2) as part of a gas mixture for carbonation.\|[0077] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes carrying out reactions in an unpressurised continuous mode to achieve substantially complete carbonation of the Magnesium Hydroxide or Magnesium silicate.\|[0078] Optionally, a non-inventive system for sequestrating Carbon Dioxide (CO2), wherein the system includes a first reaction chamber which is operable to receive a Silicate-based material and an alkaline compound, and a blending apparatus for blending contents of the first reaction chamber to produce a mixture therein.\|[0079] Optionally, the non-inventive system for sequestrating Carbon Dioxide (CO2) as described above is operable to execute the method outlined above method of sequestrating Carbon Dioxide (CO2).\|[0080] Modifications to embodiments of the invention described in the foregoing are possible without departing from the scope of the invention as defined by the accompanying claims. For example the compound in the reaction may be selected from any one or combination of Hydroxide, Carbonate, and/or Bicarbonate as would be suitable to the person skilled in the art. Expressions such as "including", "comprising", "incorporating", "consisting of", "have", "is used to describe and claim the present invention are intended to be construed in a non-exclusive manner, namely allowing for items, components or elements not explicitly described also to be present. Reference to the singular is also to be construed to relate to the plural. Numerals included within parentheses in the accompanying claims are intended to assist understanding of the claims and should not be construed in any way to limit subject matter claimed by these claims.	Family Number\|(45351908)\|45351908\|Object of Invention\|(EP3129125 B1)\|The present invention provides a method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, wherein the method comprises: a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from a group comprising alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole (...) \|Abstract\|(GB2516141 B)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) comprises heating a dry solid-solid mixture of magnesium silicate material with an alkali metal compound at a temperature below 300Â°C in an unpressurized vessel for less than 4 hours to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, and a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products. The magnesium silicate preferably comprises naturally occurring Olivine or Serpentine mineral. The magnesium hydroxide may be used to sequester carbon dioxide (CO2) to produce a metal carbonate.\|(WO2015154887 A1)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.\|(US9963351 B2)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300 C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.\|(EP3129125 B1)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.\|(CN106573197B B)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide ( CO2 ) is provided . The method includes heating a dry solid - solid mixture of an alkaline earth Silicate - based material with an alkali metal compound at a temperature below 300 C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate , wherein the Silicate - based material comprises a naturally occurring Olivine , Serpentine mineral and alkali metal silicate . The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry , comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide ( CO2 ) , producing a metal Carbonate . The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation . \|(DK3129125T T3)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300 C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.(From US9963351 B2)\|(ES2824676 T3)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300 C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.(From US9963351 B2)\|Advantages / Prev. Drawbacks\|(GB2515995 A)\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONALE RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flu Gases". \|(GB2516141 B)\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(GB2516141 A)\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(WO2015154887 A1)\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(US9963351 B2)\|Moreover, similar problems with the approach are described in US patent application 2004126192A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(US20170029284 A1)\|Moreover, similar problems with the approach are described in US patent application 2004126192A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(CN106573197B B)\|( . . . ) Therefore , there is a need to develop a carbon dioxide sequestration technology with higher energy efficiency , higher productivity , and higher cost efficiency than the prior art , and the technology can be applied to industrial production . \|(CN106573197 A)\|( . . . ) Therefore , there is a need to develop a carbon dioxide sequestration technology with higher energy efficiency , higher productivity , and higher cost efficiency than the prior art , and the technology can be applied to industrial production . \|Independent Claims\|(GB2516141 B)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal hydroxide to form a dry solid -solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid -solid mixture to a temperature below 300C (...) \|(GB2516141 A)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal compound to form a dry solid -solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid -solid mixture to a temperature below 300C (...) \|(WO2015154887 A1)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal compound to form a dry solid-solid mixture with a molar ratio in the range of 1 -3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300C (...) \|(US9963351 B2)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal hydroxide to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300 (...) \|(US20170029284 A1)\| (...) A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal hydroxide to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300 (...) \|(EP3129125 B1)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from the group consisting of alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per (...) \|(CN106573197B B)\|1. A process for activating magnesium silicate by conversion to magnesium hydroxide comprising the steps of : a . mixing the dried magnesium silicate rock powder with a dried alkali metal hydroxide powder , in a ratio of alkali metal elements in the alkali metal hydroxide : 1-3 mol of silicon element in the magnesium silicate is prepared into a dry solid mixture ; b . heating the dried solid mixture ( . . . ) \|(CN106573197 A)\|1. A process for activating magnesium silicate by conversion to magnesium hydroxide comprising the steps of : a . mixing the dried magnesium silicate rock powder with a dried alkali metal compound in a ratio of 1 : 3, preparing a dry solid mixture ; b . heating the dried solid mixture in a non - sealed pressurized container at a temperature below 300 ℃for up to 4 hours to form a glass phase mixture ( . . . ) \|	Chemical engineering\|Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-053/80\|B01D-2251/304\|B01D-2251/402\|B01D-2251/404\|B01D-2251/604\|B01D-2257/504\|B01D-2258/0283\|B01D-2259/126\|C01F-005/14\|C01F-005/22\|C01F-005/24\|C01F-011/12\|C01F-011/18\|C01P-2002/72\|C01P-2002/88\|Y02C-010/04\|Y02C-020/40\|Y02P-020/151\|Y02P-020/152		B01D-053/62\|B01D-053/80\|B01D-2251/304\|B01D-2251/402\|B01D-2251/404\|B01D-2251/604\|B01D-2257/504\|B01D-2258/0283\|B01D-2259/126\|C01F-005/14\|C01F-005/22\|C01F-005/24\|C01F-011/12\|C01F-011/18\|C01P-2002/72\|C01P-2002/88\|Y02C-010/04\|Y02C-020/40\|Y02P-020/151\|Y02P-020/152	B01D-053/62\|B01D-053/80\|B01F-003/18\|C01F-005/14\|C01F-005/22\|C01F-005/24\|C01F-011/12\|C01F-011/18	B01D-053/62\|B01D-053/80\|B01F-003/18\|C01F-005/14\|C01F-005/22\|C01F-005/24\|C01F-011/12\|C01F-011/18			CN109923068\|JP2025501392\|EP3743195\|WO2019145491;WO2019145491\|CN106365915\|CN106396746\|CN106396810\|WO201853497\|WO2025189212;WO2025189212\|CN119517198\|WO202530116\|CN115838261\|CN114560716\|EP4298057;EP4298057;EP4298057\|WO2023134849\|CN111715146\|CN111346600\|CN109734108\|CN111683732\|CN105457461\|CN105158439\|US20220127151\|US20190210883\|WO2024180441\|EP4421058\|US11896930\|US11718558\|US11718558\|US12110601\|US12110601\|US12559376\|EP3743195\|WO2019145491;WO2019145491\|FR3077008;FR3077008\|US11242261\|US10343113\|US9963351\|US9963351\|US9963351	CN109923068 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SELF=N\|US20130036948 60642622 WHO=Applicant SELF=N\|US20130036948 60642622 WHO=Examiner SELF=N\|CN103415632 62236355 WHO=Examiner SELF=N\|US20120288431 1887580 WHO=Applicant SELF=N\|CN101830475 7095205 WHO=Examiner SELF=N\|CN101679059 1841774 WHO=Examiner SELF=N\|CN101679060 1841740 WHO=Examiner SELF=N\|CN101652323 6952466 WHO=Examiner SELF=N\|US8114374 1759232 WHO=Applicant SELF=N\|US8114374 1759232 WHO=Applicant SELF=N\|US7604787 43663450 WHO=Applicant SELF=N\|US20040213705 1759232 WHO=Applicant SELF=N\|US20040213705 1759232 WHO=Examiner SELF=N\|US20040213705 1759232 WHO=Examiner SELF=N\|US20040126293 793726 WHO=Applicant SELF=N\|US5624493 42940175 WHO=Applicant SELF=N\|US5624493 42940175 WHO=Examiner SELF=N\|US4708640 2618546 WHO=Applicant SELF=N		US4708640; US5624493; XP055204425; US20120288431; US8114374\|US4708640; US5624493; US20120288431; US8114374; US7604787; US20040126293; US8114374\|\|\|CN102784570; US5624493; CN101830475; CN101652323; CN103415632; CN101679059; CN101679060\|US20150368154; US4708640; US5624493; US8114374; US20040213705; US20120288431; US20130036948; GB2515995; GB2516141; WO2015154887\|US20130036948; US20040213705\|US20040213705	(EP3129125)\|Applicant references\|-The Masters thesis by Mabell Delgado Torróntegui at ETH in Switzerland, "Assessing the Mineral carbonation science and technology" (2010\|\|(US9963351)\|Search Report references [Examiner]\|-Zevenhoven et al., “Carbon dioxide mineralisation and integration with flue gas desulfurisation applied to a modern coal fired power plant,” Proceedings of ECOS 2012—Jun. 26-29, 2012, Perugia, Italy. (Year: 2012).\|-Combined Search and Examination Report received for the United Kingdom Patent Application No. GB1306559.4, dated Oct. 7, 2013, 6 pages.\|-Combined Search and Examination Report received for the United Kingdom Patent Application No. GB1406520.5, dated Nov. 11, 2014, 5 pages.\|-Examination Report received for the United Kingdom Patent Application No. GB1406520.5, dated Mar. 21, 2016, 2 pages.\|-International Search Report and Written Opinion received for International Patent Application No. PCT/EP2015/025018, dated Jul. 31, 2015, 10 pages.\|-Zevenhoven, Ron, et al., “Carbon Storage by Mineralisation (CSM): Serpentinite Rock Carbonation via Mg(OH)2 Reaction Intermediate without CO2 Pre-Separation”, Energy Procedia, Proceedings of the 11th International Conference on Greenhouse Gas Control Technologies GHGT-11, vol. 37, Dec. 2013, pp. 5945-5954.\|\|(WO2015/154887)\|International Search Report [Examiner]\|-RON ZEVENHOVEN ET AL: "Carbon Storage by Mineralisation (CSM): Serpentinite Rock Carbonation via Mg(OH)2 Reaction Intermediate Without CO2 Pre-separation", ENERGY PROCEDIA, vol. 37, 1 January 2013 (2013-01-01), pages 5945 - 5954, XP055204425, ISSN: 1876-6102, DOI: 10.1016/j.egypro.2013.06.521\|\|\|\|\|\|	GRANTED	(EP3129125)\|GRANTED\|(US9963351)\|GRANTED\|(WO2015/154887)\|LAPSED\|(GB2516141)\|LAPSED\|(GB2515995)\|LAPSED\|(CN106573197)\|GRANTED\|(ES2824676)\|GRANTED\|(DK3129125)\|LAPSED	ALIVE	(EP3129125)\|ALIVE\|(US9963351)\|ALIVE\|(WO2015/154887)\|DEAD\|(GB2516141)\|DEAD\|(GB2515995)\|DEAD\|(CN106573197)\|ALIVE\|(ES2824676)\|ALIVE\|(DK3129125)\|DEAD	(EP3129125)\|LEGAL DETAILS FOR EP3129125\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-04-10\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP15723131\|Application date=2015-04-10\|Standardized application number=2015EP-0723131\|Event publication date=2016-10-31\|Event 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state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2020-08-05\|Event code=EP/REG\|Event code=IE/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patents granted designating Ireland\|European patent granted\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2023-04-19\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2023-04-19\|Year of payment of annual fees=9\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2025-04-22\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to 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notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MK\|MEMBER STATE LEGAL DETAILS FOR MT\|Actual or expected expiration date=2024-09-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MT\|Event publication date=2024-09-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MT\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or 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national office\|Annual fees payment date=2023-04-25\|Year of payment of annual fees=9\|Corresponding cc:\|Designated or member state=PL\|Event publication date=2026-01-23\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=PL\|MEMBER STATE LEGAL DETAILS FOR PT\|Actual or expected expiration date=2021-01-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PT\|Event publication date=2021-01-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PT\|MEMBER STATE LEGAL DETAILS FOR RO\|Actual or expected expiration date=2021-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RO\|Event publication date=2021-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RO\|MEMBER STATE LEGAL DETAILS FOR RS\|Actual or expected expiration date=2021-02-26\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RS\|Event publication date=2021-02-26\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced 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fees payment date=2023-03-30\|Year of payment of annual fees=9\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2024-12-03\|Event code=EP/REG\|Event code=SE/EUG\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|EP patent has lapsed\|EUROPEISKT PATENT HAR UPPHOERT ATT GAELLA\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2025-10-13\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=SE\|MEMBER STATE LEGAL DETAILS FOR SI\|Actual or expected expiration date=2021-08-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SI\|Event publication date=2021-08-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SI\|MEMBER STATE LEGAL DETAILS FOR SK\|Actual or expected expiration date=2021-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SK\|Event publication date=2021-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SK\|MEMBER STATE LEGAL DETAILS FOR SM\|Actual or expected expiration date=2021-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SM\|Event publication date=2021-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SM\|MEMBER STATE LEGAL DETAILS FOR TR\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=TR\|Event publication date=2023-03-30\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2023-03-30\|Year of payment of annual fees=9\|Corresponding cc:\|Designated or member state=TR\|(US9963351)\|LEGAL DETAILS FOR US9963351\|Actual or expected expiration date=2035-07-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-04-10\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US15303208\|Application date=2015-04-10\|Standardized application number=2015US-15303208\|Event publication date=2015-04-10\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:ZIMMER, ANTHONY J\|Event publication date=2015-04-10\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2015-04-10\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: CCC001US\|Event publication date=2015-04-10\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 123123\|Event publication date=2015-04-10\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2015-04-10\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2016-10-10\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2016-10-10\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2016-10-17\|Event code=US/DISCSEF\|Event group=OAI\|Electronic Information Disclosure Statement\|Event publication date=2016-10-17\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2016-10-19\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro 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code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=2018-04-18\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2018-05-08\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US09963351\|Publication stage code=B2\|Publication date=2018-05-08\|Standardized publication number=US9963351\|Event publication date=2018-05-08\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 92 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=92\|Event publication date=2021-05-18\|Event code=US/NMFP\|Event group=Payment or 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indicator=Pos\|Event group=Examination events\|Patent application filed\|Publication country=GB\|Publication number=GB201306559\|Publication stage code=D0\|Publication date=2013-05-22\|Standardized publication number=GB201306559\|Event publication date=2015-01-14\|Event code=GB/A\|Event group=Examination events\|Published Application\|Publication country=GB\|Publication number=GB2515995\|Publication stage code=A\|Publication date=2015-01-14\|Standardized publication number=GB2515995\|Event publication date=2018-02-21\|Event code=GB/WAP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application withdrawn, taken to be withdrawn or refused ** after publication under section 16(1)\|(CN106573197)\|LEGAL DETAILS FOR CN106573197\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-04-10\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN 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of patent right\|(ES2824676)\|LEGAL DETAILS FOR ES2824676\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-04-10\|Event code=ES/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ES ES15723131\|Application date=2015-04-10\|Standardized application number=2015ES-0723131T\|Event publication date=2021-05-13\|Event code=ES/T3\|Event indicator=Pos\|Event group=Event indicating In Force\|Translation of granted European patent (former B3)\|Publication country=ES\|Publication number=ES2824676\|Publication stage code=T3\|Publication date=2021-05-13\|Standardized publication number=ES2824676\|(DK3129125)\|LEGAL DETAILS FOR DK3129125\|Actual or expected expiration date=2024-04-30\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2015-04-10\|Event code=DK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=DK DK15723131\|Application date=2015-04-10\|Standardized application number=2015DK-0723131\|Event publication date=2020-10-19\|Event code=DK/T3\|Event indicator=Pos\|Event group=Event indicating In Force\|Translation of EP patent\|Publication country=DK\|Publication number=DK3129125\|Publication stage code=T3\|Publication date=2020-10-19\|Standardized publication number=DK3129125T\|Event publication date=2024-11-25\|Event code=DK/REG\|Event code=DK/EBP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|EP PATENT LAPSED\|Ep patentet bortfaldet\|Effective date of the event=2024-04-30	(EP3129125)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2015/154887)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2015/154887)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2015/154887)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2015/154887)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2015/154887)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IR, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP3129125)\|EP; DE; ES; FR; GB; IT; NL; NO; TR\|(US9963351)\|US\|(WO2015/154887)\|CN; EP; ES; US\|(CN106573197)\|CN\|(ES2824676)\|ES	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=mswdBCXrAKbh9IrHURh/U2kyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP3129125&ekey=918&xpn=EP3129125&kind=B1	https://register.epo.org/application?number=EP15723131	https://permalink.orbit.com/RenderStaticFirstPage?XPN=OOZbZWp0GcLjCoOEB2EWlnfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	GB	(WO2015/154887)\|GB	(WO2015/154887)\|NAME=CAMBRIDGE CARBON CAPTURE LTD 3 Charles Babbage Road Cambridge, Cambridgeshire CB3 0GT , COUNTRY=GB	(EP3129125)\|GB\|(EP3129125)\|GB\|(WO2015/154887)\|GB\|\|	(EP3129125)\|NAME=Norris, Timothy Sweyn;Basck 50 - 60 Station Road , CITY=Cambridge CB1 2JH , COUNTRY=GB , REG=101324986\|(EP3129125)\|NAME=Norris, Timothy Sweyn;Basck 16 Saxon Road , CITY=Cambridge CB5 8HS , COUNTRY=GB , REG=101324986\|(WO2015/154887)\|NAME=NORRIS, Timothy Sweyn Basck 9 Meadowford Newport Saffron Walden, Essex CB11 3QL , COUNTRY=GB\|(CN106573197)\|NAME=ZHU HAIYAN;TAHOTA LAW FIRM , REG=51219\|(CN106573197)\|NAME=WANG SONGLAI;BEIJING CONCEPT INTELLECTUAL PROPERTY AGENCY	(EP3129125)\|GB\|(EP3129125)\|GB\|(US9963351)\|GB\|(US20170029284)\|GB\|(WO2015/154887)\|GB\|\|\|\|(CN106573197)\|GB\|\|\|	(EP3129125)\|NAME=PRIESTNALL, Michael 3 Charles Babbage Road, CITY=CambridgeCambridgeshire CB3 0GT, COUNTRY=GB\|(EP3129125)\|NAME=PRIESTNALL, Michael 3 Charles Babbage Road, CITY=CambridgeCambridgeshire CB3 0GT, COUNTRY=GB\|(US9963351)\|NAME=Priestnall Michael, CITY=Cambridge, COUNTRY=GB\|(US20170029284)\|NAME=PRIESTNALL Michael, CITY=Cambridge, COUNTRY=GB\|(WO2015/154887)\|NAME=PRIESTNALL, Michael 3 Charles Babbage Road Cambridge, Cambridgeshire CB3 0GT, COUNTRY=GB\|(GB2516141)\|NAME=Michael Priestnall\|(GB2516141)\|NAME=MICHAEL PRIESTNALL\|(GB2515995)\|NAME=MICHAEL PRIESTNALL\|(CN106573197)\|NAME=Michael. Stena Plymouth The British Cambridge County of Cambridge city Charles Babbage Road No. 3, CITY=Cambridge, STATE=Cambridgeshire , COUNTRY=GB\|(CN106573197)\|NAME=PRIESTNALL MICHAEL\|(ES2824676)\|NAME=PRIESTNALL, Michael\|(DK3129125)\|NAME=PRIESTNALL, Michael	(WO2015/154887)\|11\|(EP3129125)\|12\|(CN106573197)\|12\|(US9963351)\|12\|(GB2516141)\|12\|(GB2515995)\|11	3	8			(EP3129125)\|WO2015/154887\|(US9963351)\|WO2015/154887\|(CN106573197)\|WO2015/154887\|(ES2824676)\|WO2015/154887\|(DK3129125)\|WO2015/154887	(ES2824676)\|EP15723131\|(DK3129125)\|EP15723131	(EP3129125)\|Number of Claims: NCL=11\|\|(US9963351)\|Number of Claims: NCL=14\|Number of Drawings: NDR=16\|Number of Figures: NFG=17\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=92\|Primary examiner: Zimmer Anthony J\|Art Unit.: ART =1736\|\|(US20170029284)\|Number of Claims: NCL=14\|Number of Drawings: NDR=16\|Number of Figures: NFG=17\|Independent Claim Number: ICL=14\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=14\|Primary examiner: Zimmer Anthony J\|Art Unit.: ART =1736\|\|(WO2015/154887)\|Number of Claims: NCL=13\|Extended kind: EXTK=x\|\|(GB2516141)\|Number of Claims: NCL=11\|\|(GB2516141)\|Number of Claims: NCL=13\|\|(GB2515995)\|Number of Claims: NCL=9\|\|(CN106573197)\|Number of Claims: NCL=11\|Gazette date: GAZDATE=2019-08-23\|Gazette number: GAZNUM=35-3402\|Substantial examination effective date: 20170517 Examination duration: 27 months\|Number of Pages: NPAGES=32\|Primary examiner: 王如军\|Primary examiner: Wang Ru Jun\|\|(CN106573197)\|Number of Claims: NCL=13\|Gazette date: GAZDATE=2017-04-19\|Gazette number: GAZNUM=33-16\|Substantial examination effective date: 20170517 Examination duration: 27 months\|Number of Pages: NPAGES=31\|Primary examiner: 王如军\|Primary examiner: Wang Ru Jun\|	(US9963351)\|Previous publication: US20170029284 A1 2017-02-02 [US20170029284]\|(CN106573197)\|Previous publication: CN106573197 A 2017-04-19 [CN106573197]	(EP3129125)\|ENGLISH (ENG)	(ES2824676)\|Patent\|(DK3129125T)\|Patent\|(EP3129125)\|Patent\|(CN106573197B)\|Patent\|(US9963351)\|Patent\|(CN106573197)\|Patent\|(EP3129125)\|Patent\|(US20170029284)\|Patent\|(GB2516141)\|Patent\|(WO2015154887)\|Patent\|(GB2515995)\|Patent\|(GB2516141)\|Patent\|(GB201406520)\|Patent\|(GB201306559)\|Patent	Titre: (EP3129125)\|Method of activation of mineral silicate minerals Résumé: (EP3129125)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.	21	Abstract	gpt-4o-mini	yes	The article describes a method for activating silicate minerals to sequester CO2 through mineral carbonation, which aligns with the topic of enhanced weathering.
23	CN202310871419	CN202310871419	CN116808978	106692037	CN116808978 A 2023-09-29 [CN116808978]	2023-07-17	2023-07-17	2023-09-29		(CN116808978)\|2025-02-21	(CN116808978)\|Kettle-type reaction device for carbonization test of building materials and application of kettle-type reaction device	(CN116808978)\|The invention provides a kettle type reaction device for a carbonization test of a building material. The kettle type reaction device comprises an airtight reaction tank body, a temperature adjusting device, a humidity adjusting device, an air pressure adjusting device, a carbon dioxide gas input device and a sensor group. The invention further provides a building material carbonization test system. The building material carbonization test system comprises the kettle type reaction device and a control center. The invention also provides an application of the building material carbonization test system in researches such as consumption of carbon dioxide waste gas, carbon immobilization in a deep ground environment, rock weathering or CO2 mineralization and the like. The building material carbonization test system disclosed by the invention has higher safety when being used for high-concentration carbonization test of the building material, the test result is more in line with the real situation, and the carbon absorption or carbon resistance of the building material under the condition of high-concentration carbon dioxide can be measured under normal pressure; the method has higher reference value for research on consumption of carbon dioxide waste gas, carbon immobilization of deep ground environment, rock weathering or CO2 mineralization and the like.	NELD INTELLIGENT TECHNOLOGY XIANGHE	(CN116808978)\|NELD INTELLIGENT TECHNOLOGY XIANGHE CO., LTD. ([CN])	ZHANG HUIYI	(CN116808978)\|ZHANG HUIYI	(CN116808978)\|LIU JUNLING;BEIJING ZHAOJUN UNION INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11333	(CN116808978)\|On the one hand, the concrete is not easy to breathe, because the binding degree of the cementing material, sand and stones in the concrete is higher after hydration reaction, the higher the strength is, the stronger the inner compactness of the concrete is, and the through holes are hardly formed, so that the outside air is difficult to smoothly diffuse into the inside of the concrete.\|	(CN116808978)\|1. A kettle reaction device for carbonization testing of building materials, comprising:the airtight reaction tank body is used as an airtight space for accommodating a test block and forming a preset environment of carbon dioxide concentration, temperature, air pressure and humidity;the temperature adjusting device is arranged in the airtight reaction tank body and used for adjusting the temperature in the airtight reaction tank body;the humidity adjusting device is used for adjusting the humidity in the airtight reaction tank body;the air pressure adjusting device is arranged on the airtight reaction tank body and is used for adjusting the air pressure in the airtight reaction tank body;the carbon dioxide gas input device is used for externally connecting carbon dioxide storage equipment and inputting carbon dioxide gas into the airtight reaction tank body;and the sensor group is used for monitoring the concentration, temperature, air pressure and humidity of the carbon dioxide in the airtight reaction tank body.\|	(CN116808978)\|A further object of the invention is: provides the kettle type reaction device for consuming carbon dioxide waste gas generated by cement plants or power plants, carbon solid storage in deep environment, rock efflorescence and CO by cement building materials 2 Mineralization and other research applications. The above object of the present invention is achieved by the following means: in a first aspect, the present invention provides a tank reactor for carbonization testing of building materials, comprising:\|The invention provides a kettle type reaction device for a carbonization test of building materials, which comprises: the device comprises an airtight reaction tank body, a temperature adjusting device, a humidity adjusting device, an air pressure adjusting device, a carbon dioxide gas input device and a sensor group. The invention also provides a carbonization test system for the building material, which comprises the kettle-type reaction device and a control center. The invention also provides the building material carbonization test system for carbon sequestration and rock weathering or CO in the deep environment consuming carbon dioxide waste gas 2 Mineralization and other research applications.\|The invention relates to a kettle type reaction device capable of providing high-concentration carbon dioxide, which uses carbon dioxide waste gas to carry out inorganic building material maintenance, carbon sequestration in deep environment, rock weathering and CO 2 Mineralization and other research applications.\|	(CN116808978)\|AIRTIGHT REACTION TANK(100,82)\|BUILDING MATERIAL(100,71)\|KETTLE TYPE REACTION(100,20)\|KETTLE REACTION(100,16)\|CARBONIZATION(100,10)\|BUILDING MATERIAL TESTING(100,2)\|REACTION TANK(60,71)\|TANK REACTOR(40,11)\|DEEP ENVIRONMENT(36,7)\|HUMIDITY(34,21)\|MINERALIZATION(34,7)\|CONCRETE CARBONIZATION TESTING(30,1)\|CONCRETE INNER COMPACTNESS(30,1)\|CARBON DIOXIDE(25,103)\|CONCRETE CARBONATION TEST(25,1)\|CIRCULATION PROMOTION(22,1)\|REGULATING HUMIDITY(22,1)\|PRESET DEVICE ENVIRONMENT(21,2)\|TOUCHSCREEN(20,9)\|CARBONIZATION TEST(20,5)\|INNER COMPACTNESS(20,1)\|PUTTING STEAM(19,1)\|CONCRETE(18,15)\|PRESSURIZED NITROGEN INLET(18,1)\|CARBON SEQUESTRATION(17,7)\|INVENTIONTHE MATERIAL CARBONIZATION(17,1)\|CARBON DIOXIDE CONCENTRATION SENSOR(16,16)\|SENSOR GROUP(16,5)\|CARBON DIOXIDE PRESET ENVIRONMENT(16,2)\|GAS INPUT(15,11)\|CARBON DIOXIDE WASTE GAS(15,9)\|EFFLORESCENCE(15,2)\|AIRTIGHT SPACE(14,4)\|CARBON DIOXIDE GAS INPUT(12,11)\|CARBON DIOXIDE GAS(12,10)\|WASTE GAS(12,9)\|CEMENT PLANT(12,4)\|ELECTROMAGNETIC VALVE(12,4)\|BUILDING MATERIAL CARBONIZATION TEST(12,1)\|STEAM INPUT(12,1)\|CARBONIZATION TEST SYSTEM(11,27)\|HUMIDITY SENSOR(11,10)\|PRESET PARAMETER CONDITION(11,3)\|STORAGE EQUIPMENT(11,3)\|CEMENT KILN FLUE GAS(11,2)\|CARBON SOLID STORAGE(11,1)\|HYDRATION REACTION(11,1)\|SAND(11,1)\|TEST CARBON ABSORPTION PERFORMANCE(11,1)\|BLOWER(10,2)\|CARBON CURING(10,2)\|EVAPORATOR(10,2)\|TEST BLOCK(9,11)\|HEATING ROD(9,6)\|CARBON DIOXIDE STORAGE EQUIPMENT(9,3)\|MAN MACHINE INTERACTION INTERFACE(9,3)\|TRAPPING(9,2)\|OUTSIDE AIR(9,1)\|CARBON MONOXIDE(8,20)\|STEAM GENERATOR(8,1)\|FAN WIND WHEEL(7,6)\|MINERALIZATION RESEARCH(7,2)\|TEMPERATURE ADJUSTMENT(7,2)\|BUILDING MATERIAL MAINTENANCE(7,1)\|AIR PRESSURE(6,26)\|HUMIDITY MEASUREMENT(6,3)\|PRESET VALUE(6,3)\|VACUUMIZING TUBE(6,3)\|CEMENT BUILDING MATERIAL(6,2)\|CURING(6,2)\|PRESSURE REDUCTION(6,1)\|INNER CONTAINER(5,13)\|PRESSURE SENSOR(5,10)\|TEMPERATURE SENSOR(5,10)\|POWER PLANT(5,6)\|CARBON DIOXIDE INPUT(5,3)\|AIR PRESSURE REGULATOR(5,1)\|CARBONATION TEST SYSTEM(5,1)\|CARBONIZATION TEST KETTLE REACTOR(5,1)\|CEMENTING MATERIAL(5,1)\|VACUUM PUMP(5,1)\|LINER(4,9)\|CONCRETE TEST BLOCK(4,5)\|CARBON DIOXIDE CONCENTRATION MEASUREMENT(4,3)\|AIR COMPRESSOR(4,2)\|BUILDING MATERIAL CARBON MAINTENANCE(4,2)\|RAPID REACTION(4,2)\|ACCELERATED WEATHERING(4,1)\|CARBONATION DEPTH(4,1)\|CARBONTHE RESEARCH(4,1)\|CEMENT ROCK(4,1)\|CEMENTING MATERIAL DEGREE(4,1)\|CONCRETE LATE STRENGTH(4,1)\|FACTOR RESEARCHING INFLUENCE(4,1)\|GEOLOGICAL SEALING(4,1)\|INFLUENCE CARBONIZATION(4,1)\|LABORATORY EQUIPMENT PERSONNEL QUALIFICATION(4,1)\|OPERATOR SKILL QUALIFICATION(4,1)\|RESEARCHER(4,1)\|VACUUMIZING PIPE(4,1)\|CONTROL CENTER(3,10)\|HIGH CONCENTRATION CARBONIZATION(3,5)\|INNER TANK(3,4)\|BAROMETER(3,3)\|HYGROMETER(3,3)\|TEMPERATURE MEASUREMENT(3,3)\|TEST RESULT(3,3)\|THERMOMETER(3,3)\|CARBON DIOXIDE CONCENTRATION METER(3,2)\|CEMENT FACTORY(3,2)\|CLOSED CONTAINER(3,2)\|DECOMPRESSION(3,2)\|CARBONIZATION BOX(3,1)\|CARBONIZATION DEPTH(3,1)\|EVACUATION PIPE(3,1)\|GEOLOGICAL STORAGE(3,1)\|TEMPERATURE REDUCTION(3,1)\|CONTROL UNIT(2,12)\|HIGH CONCENTRATION CARBON DIOXIDE(2,5)\|INTEGRATED CIRCUIT CHIP(2,4)\|OUTER SHELL(2,4)\|OUTER TANK(2,4)\|CARBON DIOXIDE ABSORPTION CAPACITY(2,3)\|CONTROL CABINET(2,3)\|DATA PROCESSING(2,3)\|PRESSURE MEASUREMENT(2,3)\|LIQUID DISCHARGE(2,2)\|ABSORBING CARBON DIOXIDE(2,1)\|CARBON COLLECTION(2,1)\|CARBON NEUTRALIZATION(2,1)\|CEMENT PRODUCTION(2,1)\|CONCENTRATION TECHNICAL MEASURE(2,1)\|CONCENTRATIONAND(2,1)\|CONCRETE CARBON DIOXIDE ABSORPTION(2,1)\|CONCRETE CARBON RESISTANCE(2,1)\|DAMP ADJUSTMENT(2,1)\|DEEP SOIL ENVIRONMENT(2,1)\|EVACUATING TUBE(2,1)\|HUMIDITY ENVIRONMENT(2,1)\|RAPID EVALUATION(2,1)\|REFRIGERATION(2,1)\|SLEEVED INSIDE(2,1)\|TECHNICAL GRADE(2,1)\|VACUUMIZING GAS(2,1)\|	(CN116808978)\|1. A kettle reaction device for carbonization testing of building materials, comprising:\|the airtight reaction tank body is used as an airtight space for accommodating a test block and forming a preset environment of carbon dioxide concentration, temperature, air pressure and humidity;\|the temperature adjusting device is arranged in the airtight reaction tank body and used for adjusting the temperature in the airtight reaction tank body;\|the humidity adjusting device is used for adjusting the humidity in the airtight reaction tank body;\|the air pressure adjusting device is arranged on the airtight reaction tank body and is used for adjusting the air pressure in the airtight reaction tank body;\|the carbon dioxide gas input device is used for externally connecting carbon dioxide storage equipment and inputting carbon dioxide gas into the airtight reaction tank body;\|and the sensor group is used for monitoring the concentration, temperature, air pressure and humidity of the carbon dioxide in the airtight reaction tank body.\|2. The kettle type reaction device as claimed in claim 1, wherein said temperature adjusting device is composed of a heating device and a refrigerating device; the heating device is a heating rod; the refrigerating device is an evaporator or a plate heat exchanger.\|3. The tank reactor according to claim 2, wherein the humidity regulator is a steam input device provided in the airtight reaction tank, and the humidity is increased by inputting steam into the airtight reaction tank via an external steam generator.\|4. The tank reactor of claim 3 wherein said air pressure regulator comprises a vacuum pump, an air compressor and/or a pressurized nitrogen inlet.\|5. The tank reactor according to any one of claims 1 to 4, wherein a blower means is provided in the airtight reaction tank for promoting circulation of gas in the airtight reaction tank.\|6. The tank reactor of claim 5 wherein said sensor set comprises a carbon dioxide concentration sensor, a temperature sensor, a pressure sensor and a humidity sensor; the temperature sensor, the pressure sensor and the humidity sensor are arranged on the airtight reaction tank body and are used for directly contacting the gas in the airtight reaction tank body; the carbon dioxide concentration sensor is arranged inside or outside the airtight reaction tank body, the carbon dioxide concentration sensor arranged inside the airtight reaction tank body is used for directly contacting the gas with the temperature lower than 50 ℃ in the airtight reaction tank body, and the carbon dioxide concentration sensor arranged outside the airtight reaction tank body is used for contacting the gas which is collected from the airtight reaction tank body and is subjected to temperature reduction and pressure reduction.\|7. A building material carbonization test system, characterized in that: comprising a tank reactor and a control center according to any one of claims 1 to 6; the control center is provided with a temperature measurement and control unit, a humidity measurement and control unit, a pressure measurement and control unit and a carbon dioxide concentration measurement and control unit, wherein each measurement and control unit respectively receives signals or data from the temperature sensor, the humidity sensor, the pressure sensor and the carbon dioxide concentration sensor, and controls the operation of the temperature adjusting device, the humidity adjusting device, the air pressure adjusting device, the carbon dioxide input device and the fan device of the kettle type reaction device through a control circuit and an electromagnetic valve, so that the airtight reaction tank body of the kettle type reaction device achieves preset parameter conditions.\|8. The building material carbonization test system according to claim 7, wherein: the control center is also provided with an integrated circuit chip and a touch screen; the touch screen can display a man-machine interaction interface, is used for displaying operation state parameters of the kettle type reaction device to an operator, and is used for inputting parameters and instructions by the operator; the integrated circuit chip utilizes an embedded program to complete data processing and control of each measurement and control unit and the touch screen.\|9. Use of the carbonization testing system for concrete carbonization testing building material according to any one of claims 7 or 8 for high concentration carbonization testing of building material, characterized in that: placing a building material test block in an airtight reaction tank body of a kettle-type reaction device of a building material carbonization test system, firstly vacuumizing the airtight reaction tank body to negative pressure through a vacuumizing device of the kettle-type reaction device, rapidly filling carbon dioxide gas into the airtight reaction tank body through a pressurized carbon dioxide gas input device of the kettle-type reaction device, enabling the air pressure in the airtight reaction tank body to reach normal pressure and the carbon dioxide concentration to reach more than 90%, and then adjusting the temperature, humidity and air pressure in the airtight reaction tank body to reach preset values through a temperature adjusting device, a humidity adjusting device and an air pressure adjusting device of the kettle-type reaction device based on detection of a sensor group of the kettle-type reaction device, and observing the carbon absorption performance of the test block according to a conventional method.\|10. Use of the concrete carbonation test building material carbonation test system according to any one of claims 7 or 8 and for consuming carbon dioxide waste gas generated by a cement plant or a power plant, characterized in that: the building material carbonization test system is used for carbon maintenance of building materials; the method specifically comprises the following steps: CO of cement kiln flue gas 2 After trapping, carbon dioxide gas is input into the airtight reaction tank body through the carbon dioxide gas input device of the carbonization test system for building materials according to any one of claims 7 or 8 to carry out carbon curing on the building materials, and the curing process is completed by carrying out constant pressure rapid reaction at the pressure of 1bar-15bar and the normal temperature for 2 hours.	(CN116808978)\|TECHNICAL FIELD\|[0001] The invention relates to a kettle type reaction device capable of providing high-concentration carbon dioxide, which uses carbon dioxide waste gas to carry out inorganic building material maintenance, carbon sequestration in deep environment, rock weathering and CO 2 Mineralization and other research applications.\|BACKGROUND ART\|[0002] "Green" low carbonThe research and development of cement production technology, namely low-carbon/ultra-low-carbon concrete in the field of building materials, is a hot spot of research and development at the present stage. Meanwhile, in view of the fact that the carbon dioxide is absorbed and utilized by the concrete after being captured, the strength of the concrete can be greatly improved, so that how to achieve carbon neutralization and improve the strength of building materials in the building material industry is a new hot spot for research in the industry. Furthermore, for technical grade CO 2 The carbon collection and deep-ground carbon sequestration technology is also of great significance for realizing 'double carbon targets', wherein factors such as deep-ground environment temperature, pressure and the like influence carbonization rules and CO in different stratum environments 2 The problems of stability, temperature, pressure and the like are worthy of intensive research.\|[0003] In the development of "carbon-neutral" production technology and deep-ground carbon sequestration technology for building materials, in particular inorganic building materials, research into carbonization of concrete has been involved. The carbonization of concrete means that carbon dioxide in air and calcium hydroxide in cement stone are subjected to chemical action under the condition of existence of water to generate calcium carbonate and water. The carbonization process is a process that carbon dioxide gradually diffuses from the surface to the inside of the concrete. The most important effect of carbonization on concrete is: the early strength and the later strength of the concrete are improved rapidly, the deeper the carbonization depth is, the higher the strength of the concrete is, and the different carbon dioxide absorption capacities of different mixing ratios of the concrete can be embodied through the carbonization process. In order to match with the consumption of carbon dioxide waste gas, the CO of the concrete under the high-temperature and high-pressure conditions in the research and development of being absorbed by the concrete and the geological storage technology 2 The carbon absorption and carbon resistance of the concrete are required to be detected through a carbonization test.\|[0004] The alkaline component in the concrete material can be mixed with CO with the concentration of 0.04% in the atmosphere under the natural condition 2 The chemical reaction is carried out but the process is very slow, with the depth of carbonation generally "no more than" 10 mm over its life cycle. But can quickly realize concrete carbonization by the technical measures of concentration improvement, temperature rise, pressurization and the like, and the strength of the product is higher. In the prior art, the carbonization test process of concrete generally comprises the steps of delivering carbon dioxide-containing gas with a certain concentrationAnd (3) placing the sample into a closed container for holding the concrete test block, and observing the depth of carbon dioxide absorbed by the test block or permeated and diffused into the test block within a certain time. For the study of carbon dioxide absorption of concrete, the carbonization test for measuring carbon absorption performance thereof requires the use of high concentration carbon dioxide gas. In the current practice, a high-concentration high-pressure high-temperature carbonization box is used for concrete carbonization test, high-concentration carbon dioxide is pressed into concrete by using the pressure of high-pressure gas, and the absorption and neutralization effects of the concrete on the carbon dioxide are observed. The high pressure of the gas in this test is usually generated by charging a large amount of carbon dioxide gas into a closed container containing air in order to achieve a sufficiently high carbon dioxide concentration, and the gas is also used by the test person as a driving force for absorbing carbon dioxide in concrete. However, such high pressure tests not only require a high pressure resistant container, but also have special requirements for the skill qualification of the operators, which would otherwise present a significant production safety risk.\|DISCLOSURE\|Disclosure of Invention\|[0005] In view of the above technical background, a primary object of the present invention is: the kettle type reaction device for the carbonization test of the building material can provide a high-concentration carbon dioxide environment and has higher safety.\|[0006] A further object of the invention is: provides the kettle type reaction device for consuming carbon dioxide waste gas generated by cement plants or power plants, carbon solid storage in deep environment, rock efflorescence and CO by cement building materials 2 Mineralization and other research applications.\|[0007] The above object of the present invention is achieved by the following means:\|in a first aspect, the present invention provides a tank reactor for carbonization testing of building materials, comprising:\|the airtight reaction tank body is used as an airtight space for accommodating a test block and forming a preset environment of carbon dioxide concentration, temperature, air pressure and humidity;\|the temperature adjusting device is arranged in the airtight reaction tank body and used for adjusting the temperature in the airtight reaction tank body;\|the humidity adjusting device is used for adjusting the humidity in the airtight reaction tank body;\|the air pressure adjusting device is arranged on the airtight reaction tank body and is used for adjusting the air pressure in the airtight reaction tank body;\|the carbon dioxide gas input device is used for externally connecting carbon dioxide storage equipment and inputting carbon dioxide gas into the airtight reaction tank body;\|and the sensor group is used for monitoring the concentration, temperature, air pressure and humidity of the carbon dioxide in the airtight reaction tank body.\|[0008] In the tank reactor according to the present invention, the size, shape and material of the airtight reaction tank are not particularly limited, but it is necessary to have airtightness to maintain the pressure and concentration of the internal gas and to have a certain strength to avoid deformation due to the pressure difference between the inside and outside thereof.\|[0009] In the kettle-type reaction device, the temperature adjusting device consists of a heating device and a refrigerating device; the heating device can be a heating rod and the like; the refrigeration device may be an evaporator or the like.\|[0010] In the kettle-type reaction device, the humidity adjusting device is a water vapor input device arranged on the airtight reaction tank body, and water vapor is input into the airtight reaction tank body through an external water vapor generating device to increase the humidity.\|[0011] In the kettle-type reaction device, the air pressure adjusting device at least comprises a vacuumizing device. In a further preferred scheme, the air pressure adjusting device can further comprise an external air compressor, a nitrogen input device with pressure and the like.\|[0012] In the tank reactor according to a further preferred aspect of the present invention, a blower device is provided in the airtight reaction tank to promote circulation of the gas in the airtight reaction tank in order to uniformly mix the gas in the airtight reaction tank.\|[0013] In the kettle-type reaction device, the sensor group comprises a carbon dioxide concentration sensor, a temperature sensor, a pressure sensor and a humidity sensor. The temperature sensor, the pressure sensor and the humidity sensor are arranged on the airtight reaction tank body and are used for directly contacting the gas in the airtight reaction tank body; the carbon dioxide concentration sensor is arranged inside or outside the airtight reaction tank body, the carbon dioxide concentration sensor arranged inside the airtight reaction tank body is used for directly contacting the gas with the temperature lower than 50 ℃ in the airtight reaction tank body, and the carbon dioxide concentration sensor arranged outside the airtight reaction tank body is used for contacting the gas which is collected from the airtight reaction tank body and is subjected to cooling and decompression after the gas with the temperature higher than 50 ℃ is collected.\|[0014] In a preferred embodiment of the present invention, the inner space of the airtight reaction tank is divided into two communicating areas: the test block placing area and the gas mixing area; the test block placing area is used for intensively placing one or more than two test blocks, the sensor group is directly contacted with the gas of the test block placing area, and the vacuumizing device is used for vacuumizing the gas of the test block placing area; the gas mixing area is used for receiving water vapor and carbon dioxide gas from the outside of the airtight reaction tank body and heating the gas, the temperature adjusting device is arranged in the gas mixing area, and the water vapor input device and the carbon dioxide gas input device are both opened in the gas mixing area.\|[0015] In a preferred embodiment of the present invention, in order to better reduce heat dissipation by conduction from the inside of the airtight reaction tank to the outside, the airtight reaction tank is composed of an inner tank and an outer tank, the inner tank is nested in the outer tank, and a gap is left between the inner tank and the outer tank. In a more preferable scheme, the inner tank body and the outer tank body are fixedly connected through a plurality of devices which are mutually connected in a screwed mode.\|[0016] In a further preferred scheme of the invention, in order to more flexibly adjust the air pressure and the carbon dioxide concentration in the airtight reaction tank body, the airtight reaction tank body is also provided with a nitrogen or air input device; in a more preferred embodiment, the nitrogen or air inlet means is open to the gas mixing zone.\|[0017] In a further preferred scheme of the invention, the airtight reaction tank body is also provided with an exhaust device and a liquid discharge device which are used for discharging gas and liquid in the airtight reaction tank body.\|[0018] In a further preferred scheme of the invention, the airtight reaction tank body is also provided with a safety valve.\|[0019] On the basis, the invention also provides a carbonization test system for building materials, which comprises the kettle-type reaction device and a control center; the control center is provided with a temperature measurement and control unit, a humidity measurement and control unit, a pressure measurement and control unit and a carbon dioxide concentration measurement and control unit, wherein each measurement and control unit respectively receives signals or data from the temperature sensor, the humidity sensor, the pressure sensor and the carbon dioxide concentration sensor, and controls the operation of the temperature adjusting device, the humidity adjusting device, the air pressure adjusting device, the carbon dioxide input device and the fan device of the kettle type reaction device through a control circuit and an electromagnetic valve, so that the airtight reaction tank body of the kettle type reaction device achieves preset parameter conditions.\|[0020] In the preferred scheme of the invention, the control center of the building material carbonization test system is also provided with an integrated circuit chip and a touch screen; the touch screen can display a man-machine interaction interface, is used for displaying operation state parameters of the kettle type reaction device to an operator, and is used for inputting parameters and instructions by the operator; the integrated circuit chip utilizes an embedded program to complete data processing and control of each measurement and control unit and the touch screen.\|[0021] The carbonization test system of the building material has higher safety when being used for high-concentration carbonization test of the building material, the test result is more in accordance with the actual situation, the carbon absorption or carbon resistance of the building material under the condition of high-concentration carbon dioxide can be measured under normal pressure, and the carbon waste gas consumed by cement building materials, carbon fixation in deep environment, rock weathering or CO (carbon monoxide) can be consumed 2 The research of mineralization and the like has higher reference value.\|[0022] In a second aspect, the invention also provides a carbonization test system for building materials, which consumes carbon dioxide waste gas generated by cement factories or power plants, carbon sequestration in deep environments and rock weathering orCO 2 Mineralization and other research applications.\|[0023] In a preferred application of the invention, the building material carbonization test system is used for high-concentration carbonization test of building materials, and comprises the following steps: the building material test block is placed in an airtight reaction tank body of a kettle type reaction device of the building material carbonization test system, the airtight reaction tank body is vacuumized to negative pressure through a vacuumizing device of the kettle type reaction device, then carbon dioxide gas is rapidly filled into the airtight reaction tank body through a carbon dioxide gas input device of the kettle type reaction device, so that the air pressure in the airtight reaction tank body reaches normal pressure and the carbon dioxide concentration reaches more than 90%, then the temperature, the humidity and the air pressure in the airtight reaction tank body are regulated to reach preset values through a temperature regulating device, a humidity regulating device and an air pressure regulating device of the kettle type reaction device based on detection of a sensor group of the kettle type reaction device, and then the carbon absorption performance of the test block is observed according to a conventional method.\|[0024] In the preferred application of the invention, the application of the building material carbonization test system in consuming carbon dioxide waste gas generated by cement plants or power plants is to use the building material carbonization test system for carbon maintenance of building materials. The specific steps can be as follows: CO of cement kiln flue gas 2 After trapping, carbon dioxide is input into the airtight reaction tank body through the carbon dioxide input device of the building material carbonization test system, the building material is subjected to carbon curing, and the building material is subjected to constant pressure rapid reaction at the pressure of 1bar-15bar interval and normal temperature for 2 hours, so that the curing process is completed. Not only can greatly save maintenance cost, but also the building material can absorb CO 2 The post strength is obviously increased, and the obvious advantage of low carbon benefit can be reflected while the smoke is consumed.\|[0025] In the preferred application of the invention, the application of the building material carbonization test system in consuming carbon dioxide waste gas generated by cement plants or power plants is to use the building material carbonization test system in the study of durability of building materials. The carbonization test system for the building material can accelerate carbonization of a test piece of the building material by improving the temperature and the pressure of the test environment, thereby achieving the purpose of shortening the test period.\|[0026] In the application of the invention, the application of the building material carbonization test system in carbon sequestration in deep ground environment is that the building material carbonization test system is used as a test device for: (1) research on CO of inorganic building materials under high-temperature and high-pressure conditions 2 (2) researching influence of factors such as temperature, pressure and the like on carbonization rules, (3) researching CO under different stratum environments 2 Stable temperature and pressure relationship to promote the carbon sink technology, geological sealing technology or rock efflorescence and CO of inorganic building materials 2 Research on mineralization technology.\|[0027] In a preferred application of the invention, the building material carbonization test system is used for rock weathering or CO 2 The application in mineralization is to use the building material carbonization test system as a test device for simulating accelerated weathering and CO under high temperature and high pressure 2 Mineralization process for research of how to accelerate and enlarge CO 2 Is stable and stable.\|[0028] In the art, it is conventionally considered that the carbon dioxide absorption capacity of concrete needs to be tested in a high pressure state, but the inventors considered that from the principle that carbon dioxide enters and reacts in concrete, a more realistic carbon dioxide absorption capacity of concrete can be obtained by testing in high concentration carbon dioxide gas at normal pressure. On the one hand, the concrete is not easy to breathe, because the binding degree of the cementing material, sand and stones in the concrete is higher after hydration reaction, the higher the strength is, the stronger the inner compactness of the concrete is, and the through holes are hardly formed, so that the outside air is difficult to smoothly diffuse into the inside of the concrete. On the other hand, however, there are numerous blind holes in the concrete, in which air is present, which also acts as a barrier to the penetration of external gases into the interior. In the traditional high-concentration concrete carbonization test, the test condition is high pressure, air in the blind hole is not only not easy to discharge under the existence of external high pressure, but also can be compressed, so that the concentration of carbon dioxide in the blind hole of the concrete test block and the concentration of carbon dioxide outside the blind hole have great difference in the test process, and the external carbon dioxide is not easy to enter the blind hole and is fully absorbed. Although each blind hole has limited space, the overall impact on the carbon absorption capacity of the block will be significant when a large number of distributed blind holes in the block are not capable of sufficiently absorbing carbon dioxide.\|[0029] The testing method adopts the mode of vacuumizing firstly and filling the carbon dioxide later, and before filling the carbon dioxide, the gas in the blind hole in the concrete test block can be well discharged under the negative pressure state, a vacuum body is formed, the carbon dioxide can be easily sucked into the concrete test block after filling and can smoothly permeate into each corner and each hole in the concrete test block, and when the carbon dioxide is filled to reach normal pressure, the concentration of the carbon dioxide in the blind hole in the concrete is basically consistent with the concentration measured by an external sensor. This solves two problems: 1) Carbon dioxide can enter the concrete more easily after negative pressure is formed in the test block, and the absorption rate of the carbon dioxide can be rapidly measured, so that rapid evaluation is realized; 2) The potential safety hazard caused by positive pressure or high pressure can be reduced by testing under normal pressure, and the requirements on the bearing capacity and personnel qualification of laboratory equipment are greatly reduced. The carbonization test is generally carried out in a university or research institution, and if the carbonization test can meet the test requirement of high concentration under normal pressure, the test risk can be greatly reduced.\|[0030] Based on the same principle, the test method disclosed by the invention is also applicable to carbonization tests of other inorganic building materials with porous structures.\|DRAWINGS DESCRIPTION\|[0031] FIG. 1 is a schematic view showing the overall structure of the tank reactor according to example 1.\|[0032] FIGS. 2 and 3 are schematic views showing the overall internal structure of the tank reactor according to example 1, taken from different angles.\|[0033] FIG. 4 is a schematic view showing the overall structure of the carbonization test system for a building material according to example 2.\|INVENTION MODE\|Detailed Description\|[0034] In order that the above-recited objects, features and advantages of the present invention will become more apparent, a more particular description of the invention, briefly summarized below, may be had by way of example only, by reference to the appended drawings.\|[0035] In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, but the present invention may be practiced in other ways other than those described herein, and persons skilled in the art will readily appreciate that the present invention is not limited to the specific embodiments disclosed below.\|[0036] In the following detailed description of the embodiments of the present invention, reference is made to the accompanying drawings, which form a part hereof, and in which is shown by way of illustration only, the scope of the invention is not limited by the claims. In addition, the three-dimensional dimensions of length, width and depth should be included in actual fabrication.\|[0037] Example 1 building Material carbonization test kettle reactor\|A kettle type reaction device for carbonization test of building materials has an integral structure shown in figure 1 and comprises an airtight reaction tank body, wherein one end of a shell 100 of the airtight reaction tank body is provided with a sealing cover 101, and the other end of the shell is provided with a fan wind wheel 102. The top of the housing 100 is provided with a barometer 103, a thermometer 104, a hygrometer 105, an exhaust pipe 106, a carbon dioxide concentration sensor (not shown in the figure), and a safety valve 107. The housing 100 is provided with a carbon dioxide gas input pipe 108, an evacuation pipe 109, a water vapor input pipe 110, and an air or nitrogen gas input pipe 111 on the side. A drain 112 (not shown in fig. 1) is also provided at the bottom of the housing 100.\|[0038] As shown in fig. 2 and 3, the inner container 200 is further sleeved inside the outer shell 100 of the airtight reaction tank body, and a certain gap exists between the outer shell 100 and the inner container 200 and is fixedly connected through a plurality of through connectors 300. The inner container 200 is generally divided into a test block placing area and a gas mixing area, and a semi-closed partition board is arranged in the middle; the test block placing area is internally provided with a test block frame 201, and test blocks can be placed on the test block frame 201. The evacuating tube 109 arranged on the outer shell 100 penetrates into the inner container 200 and is opened in the test block placing area, and the pressure gauge 103, the temperature gauge 104 and the humidity gauge 105 arranged on the outer shell 100 are respectively connected with the pressure sensor, the temperature sensor 203 and the humidity sensor 204 arranged in the test block placing area in the inner container 200. A heating rod 205, a fan cover 206 and a plate heat exchanger 207 are arranged in the gas mixing zone. The carbon dioxide gas input pipe 108, the water vapor input pipe 110, the air input pipe 111, and the liquid discharge pipe 112 provided on the housing 100 are all inserted into the inner container 200 and opened in the gas mixing region.\|[0039] The pressure sensor, the temperature sensor 203 and the humidity sensor 204 are used for directly contacting the gas inside the liner 200; the carbon dioxide concentration sensor can be arranged inside or outside the airtight reaction tank body according to the requirement, and when the temperature of the gas inside the airtight reaction tank body is lower than 50 ℃, the carbon dioxide concentration sensor can be arranged inside and used for directly contacting the gas inside the liner 200; when the temperature of the gas in the airtight reaction tank body is greater than or equal to 50 ℃, the carbon dioxide concentration sensor is arranged outside the airtight reaction tank body and is used for contacting the gas which is collected from the airtight reaction tank body and then subjected to cooling and decompression.\|[0040] When the kettle type reaction device is used for carbonization reaction of building materials, the airtight reaction tank body formed by the shell 100, the sealing cover 101 and the liner 200 can provide an airtight space for accommodating test blocks and keep preset carbon dioxide concentration, temperature, air pressure and humidity environments; the heating rod 205, the fan wind wheel 102 and the plate heat exchanger 207 can be used as temperature adjusting devices for adjusting the temperature of the gas in the inner container 200 of the airtight reaction tank body; in addition, the fan wind wheel 102 can also be used for uniformly mixing the gas in the liner 200 to promote the circulation of the gas in the liner 200; the water vapor input pipe 110, the fan wind wheel 102 and the plate heat exchanger 207 are used as humidity adjusting devices for adjusting the humidity of the gas in the inner container 200 of the airtight reaction tank body; the vacuumizing tube 109, the exhaust tube 106 and the air (or nitrogen) input tube 111 together form an air pressure adjusting device which can be used for adjusting the pressure of the air in the inner container 200 of the airtight reaction tank body; the barometer 103, the thermometer 104, the hygrometer 105 and the carbon dioxide concentration meter form a sensor group together with a pressure sensor, a temperature sensor 203, a humidity sensor 204 and a carbon dioxide concentration sensor which are respectively connected with the barometer 103, the thermometer 104, the hygrometer 105 and the carbon dioxide concentration meter, and the sensor group is used for monitoring the air pressure, the temperature, the humidity and the carbon dioxide concentration in the liner 200; the carbon dioxide gas input pipe 108 is used for externally connecting carbon dioxide storage equipment, and inputting carbon dioxide gas into the inner container 200 of the airtight reaction tank body so as to reach the preset carbon dioxide gas concentration; the drain pipe 112 is used to drain the liquid accumulated at the bottom of the liner 200.\|[0041] Example 2 carbonization test System for building Material\|A carbonization test system for building materials has an overall structure shown in FIG. 4, and comprises a kettle-type reaction device and a control center as described in example 1; the control center is provided with a control cabinet 400, a control circuit board is arranged in the control cabinet 400, and a temperature measurement and control module, a humidity measurement and control module, a pressure measurement and control module, a carbon dioxide concentration measurement and control module, a control circuit and a chip are arranged on the control circuit board. The touch screen 401 capable of performing man-machine interaction is arranged outside the control cabinet 400. Each measurement and control module is electrically connected with a corresponding sensor of the kettle-type reaction device through an electric wire and an electromagnetic valve respectively, receives signals or data from the corresponding sensor, and controls the operation of a fan wind wheel 102, a water vapor input pipe 110, a heating rod 205, a plate heat exchanger 207, a vacuumizing pipe 109, an exhaust pipe 106, an air (or nitrogen) input pipe 111 and a carbon dioxide gas input pipe 108 of the kettle-type reaction device through a control circuit and the electromagnetic valve, so that the airtight reaction tank body of the kettle-type reaction device achieves preset parameter conditions. The touch screen 401 may display a man-machine interaction interface for displaying operation state parameters of the tank reactor to an operator, and for inputting parameters and instructions by the operator; the chip utilizes the embedded program to complete data processing and control of each measurement and control module and the touch screen.\|[0042] The building material carbonization test system of the embodiment has higher safety when being used for high-concentration carbonization test of building materials, the test result is more in accordance with the actual situation, the carbon absorption or carbon resistance of the building materials under the condition of high-concentration carbon dioxide can be measured under normal pressure, and the carbon waste gas generated by cement factories or power plants, carbon fixation of deep environments and rock weathering or CO are consumed 2 The research of mineralization and the like has higher reference value.\|[0043] Example 3 high concentration carbonization test method for building Material\|A high-concentration carbonization testing method for building materials adopts the system of the embodiment 2 of the invention, and comprises the following steps:\|the prepared test blocks of the building material are intensively placed on the test block holder 201 in the liner 200, and then the sealing cover 101 is closed and locked, so that an airtight space is formed inside the liner 200. Before testing, the inside of the inner container 200 of the airtight reaction tank body is vacuumized to negative pressure through the vacuumizing tube 109 of the kettle type reaction device, then the carbon dioxide gas is rapidly filled into the inner container 200 through the carbon dioxide gas input tube 108 on the airtight reaction tank body, so that the air pressure in the inner container 200 of the airtight reaction tank body reaches normal pressure and the carbon dioxide concentration reaches more than 90%, then based on the detection of the pressure sensor, the temperature sensor 203, the humidity sensor 204 and the carbon dioxide concentration sensor, the control center controls the operation of the fan wind wheel 102, the water vapor input tube 110, the heating rod 205, the plate heat exchanger 207, the vacuumizing tube 109, the exhaust tube 106, the air input tube 111 and the carbon dioxide gas input tube 108 according to the embedded programs and algorithms of the chips, so that the temperature, the humidity and the air pressure in the airtight reaction tank body reach preset values, and then the carbon absorption performance of the building material test block is observed according to the conventional method.	(CN116808978)\|TECHNICAL FIELD\|[0001] The invention relates to a kettle type reaction device capable of providing high-concentration carbon dioxide, which uses carbon dioxide waste gas to carry out inorganic building material maintenance, carbon sequestration in deep environment, rock weathering and CO 2 Mineralization and other research applications.\|BACKGROUND ART\|[0002] "Green" low carbonThe research and development of cement production technology, namely low-carbon/ultra-low-carbon concrete in the field of building materials, is a hot spot of research and development at the present stage. Meanwhile, in view of the fact that the carbon dioxide is absorbed and utilized by the concrete after being captured, the strength of the concrete can be greatly improved, so that how to achieve carbon neutralization and improve the strength of building materials in the building material industry is a new hot spot for research in the industry. Furthermore, for technical grade CO 2 The carbon collection and deep-ground carbon sequestration technology is also of great significance for realizing 'double carbon targets', wherein factors such as deep-ground environment temperature, pressure and the like influence carbonization rules and CO in different stratum environments 2 The problems of stability, temperature, pressure and the like are worthy of intensive research.\|[0003] In the development of "carbon-neutral" production technology and deep-ground carbon sequestration technology for building materials, in particular inorganic building materials, research into carbonization of concrete has been involved. The carbonization of concrete means that carbon dioxide in air and calcium hydroxide in cement stone are subjected to chemical action under the condition of existence of water to generate calcium carbonate and water. The carbonization process is a process that carbon dioxide gradually diffuses from the surface to the inside of the concrete. The most important effect of carbonization on concrete is: the early strength and the later strength of the concrete are improved rapidly, the deeper the carbonization depth is, the higher the strength of the concrete is, and the different carbon dioxide absorption capacities of different mixing ratios of the concrete can be embodied through the carbonization process. In order to match with the consumption of carbon dioxide waste gas, the CO of the concrete under the high-temperature and high-pressure conditions in the research and development of being absorbed by the concrete and the geological storage technology 2 The carbon absorption and carbon resistance of the concrete are required to be detected through a carbonization test.\|[0004] The alkaline component in the concrete material can be mixed with CO with the concentration of 0.04% in the atmosphere under the natural condition 2 The chemical reaction is carried out but the process is very slow, with the depth of carbonation generally "no more than" 10 mm over its life cycle. But can quickly realize concrete carbonization by the technical measures of concentration improvement, temperature rise, pressurization and the like, and the strength of the product is higher. In the prior art, the carbonization test process of concrete generally comprises the steps of delivering carbon dioxide-containing gas with a certain concentrationAnd (3) placing the sample into a closed container for holding the concrete test block, and observing the depth of carbon dioxide absorbed by the test block or permeated and diffused into the test block within a certain time. For the study of carbon dioxide absorption of concrete, the carbonization test for measuring carbon absorption performance thereof requires the use of high concentration carbon dioxide gas. In the current practice, a high-concentration high-pressure high-temperature carbonization box is used for concrete carbonization test, high-concentration carbon dioxide is pressed into concrete by using the pressure of high-pressure gas, and the absorption and neutralization effects of the concrete on the carbon dioxide are observed. The high pressure of the gas in this test is usually generated by charging a large amount of carbon dioxide gas into a closed container containing air in order to achieve a sufficiently high carbon dioxide concentration, and the gas is also used by the test person as a driving force for absorbing carbon dioxide in concrete. However, such high pressure tests not only require a high pressure resistant container, but also have special requirements for the skill qualification of the operators, which would otherwise present a significant production safety risk.\|DISCLOSURE\|Disclosure of Invention\|[0005] In view of the above technical background, a primary object of the present invention is: the kettle type reaction device for the carbonization test of the building material can provide a high-concentration carbon dioxide environment and has higher safety.\|[0006] A further object of the invention is: provides the kettle type reaction device for consuming carbon dioxide waste gas generated by cement plants or power plants, carbon solid storage in deep environment, rock efflorescence and CO by cement building materials 2 Mineralization and other research applications.\|[0007] The above object of the present invention is achieved by the following means:\|in a first aspect, the present invention provides a tank reactor for carbonization testing of building materials, comprising:\|the airtight reaction tank body is used as an airtight space for accommodating a test block and forming a preset environment of carbon dioxide concentration, temperature, air pressure and humidity;\|the temperature adjusting device is arranged in the airtight reaction tank body and used for adjusting the temperature in the airtight reaction tank body;\|the humidity adjusting device is used for adjusting the humidity in the airtight reaction tank body;\|the air pressure adjusting device is arranged on the airtight reaction tank body and is used for adjusting the air pressure in the airtight reaction tank body;\|the carbon dioxide gas input device is used for externally connecting carbon dioxide storage equipment and inputting carbon dioxide gas into the airtight reaction tank body;\|and the sensor group is used for monitoring the concentration, temperature, air pressure and humidity of the carbon dioxide in the airtight reaction tank body.\|[0008] In the tank reactor according to the present invention, the size, shape and material of the airtight reaction tank are not particularly limited, but it is necessary to have airtightness to maintain the pressure and concentration of the internal gas and to have a certain strength to avoid deformation due to the pressure difference between the inside and outside thereof.\|[0009] In the kettle-type reaction device, the temperature adjusting device consists of a heating device and a refrigerating device; the heating device can be a heating rod and the like; the refrigeration device may be an evaporator or the like.\|[0010] In the kettle-type reaction device, the humidity adjusting device is a water vapor input device arranged on the airtight reaction tank body, and water vapor is input into the airtight reaction tank body through an external water vapor generating device to increase the humidity.\|[0011] In the kettle-type reaction device, the air pressure adjusting device at least comprises a vacuumizing device. In a further preferred scheme, the air pressure adjusting device can further comprise an external air compressor, a nitrogen input device with pressure and the like.\|[0012] In the tank reactor according to a further preferred aspect of the present invention, a blower device is provided in the airtight reaction tank to promote circulation of the gas in the airtight reaction tank in order to uniformly mix the gas in the airtight reaction tank.\|[0013] In the kettle-type reaction device, the sensor group comprises a carbon dioxide concentration sensor, a temperature sensor, a pressure sensor and a humidity sensor. The temperature sensor, the pressure sensor and the humidity sensor are arranged on the airtight reaction tank body and are used for directly contacting the gas in the airtight reaction tank body; the carbon dioxide concentration sensor is arranged inside or outside the airtight reaction tank body, the carbon dioxide concentration sensor arranged inside the airtight reaction tank body is used for directly contacting the gas with the temperature lower than 50 ℃ in the airtight reaction tank body, and the carbon dioxide concentration sensor arranged outside the airtight reaction tank body is used for contacting the gas which is collected from the airtight reaction tank body and is subjected to cooling and decompression after the gas with the temperature higher than 50 ℃ is collected.\|[0014] In a preferred embodiment of the present invention, the inner space of the airtight reaction tank is divided into two communicating areas: the test block placing area and the gas mixing area; the test block placing area is used for intensively placing one or more than two test blocks, the sensor group is directly contacted with the gas of the test block placing area, and the vacuumizing device is used for vacuumizing the gas of the test block placing area; the gas mixing area is used for receiving water vapor and carbon dioxide gas from the outside of the airtight reaction tank body and heating the gas, the temperature adjusting device is arranged in the gas mixing area, and the water vapor input device and the carbon dioxide gas input device are both opened in the gas mixing area.\|[0015] In a preferred embodiment of the present invention, in order to better reduce heat dissipation by conduction from the inside of the airtight reaction tank to the outside, the airtight reaction tank is composed of an inner tank and an outer tank, the inner tank is nested in the outer tank, and a gap is left between the inner tank and the outer tank. In a more preferable scheme, the inner tank body and the outer tank body are fixedly connected through a plurality of devices which are mutually connected in a screwed mode.\|[0016] In a further preferred scheme of the invention, in order to more flexibly adjust the air pressure and the carbon dioxide concentration in the airtight reaction tank body, the airtight reaction tank body is also provided with a nitrogen or air input device; in a more preferred embodiment, the nitrogen or air inlet means is open to the gas mixing zone.\|[0017] In a further preferred scheme of the invention, the airtight reaction tank body is also provided with an exhaust device and a liquid discharge device which are used for discharging gas and liquid in the airtight reaction tank body.\|[0018] In a further preferred scheme of the invention, the airtight reaction tank body is also provided with a safety valve.\|[0019] On the basis, the invention also provides a carbonization test system for building materials, which comprises the kettle-type reaction device and a control center; the control center is provided with a temperature measurement and control unit, a humidity measurement and control unit, a pressure measurement and control unit and a carbon dioxide concentration measurement and control unit, wherein each measurement and control unit respectively receives signals or data from the temperature sensor, the humidity sensor, the pressure sensor and the carbon dioxide concentration sensor, and controls the operation of the temperature adjusting device, the humidity adjusting device, the air pressure adjusting device, the carbon dioxide input device and the fan device of the kettle type reaction device through a control circuit and an electromagnetic valve, so that the airtight reaction tank body of the kettle type reaction device achieves preset parameter conditions.\|[0020] In the preferred scheme of the invention, the control center of the building material carbonization test system is also provided with an integrated circuit chip and a touch screen; the touch screen can display a man-machine interaction interface, is used for displaying operation state parameters of the kettle type reaction device to an operator, and is used for inputting parameters and instructions by the operator; the integrated circuit chip utilizes an embedded program to complete data processing and control of each measurement and control unit and the touch screen.\|[0021] The carbonization test system of the building material has higher safety when being used for high-concentration carbonization test of the building material, the test result is more in accordance with the actual situation, the carbon absorption or carbon resistance of the building material under the condition of high-concentration carbon dioxide can be measured under normal pressure, and the carbon waste gas consumed by cement building materials, carbon fixation in deep environment, rock weathering or CO (carbon monoxide) can be consumed 2 The research of mineralization and the like has higher reference value.\|[0022] In a second aspect, the invention also provides a carbonization test system for building materials, which consumes carbon dioxide waste gas generated by cement factories or power plants, carbon sequestration in deep environments and rock weathering orCO 2 Mineralization and other research applications.\|[0023] In a preferred application of the invention, the building material carbonization test system is used for high-concentration carbonization test of building materials, and comprises the following steps: the building material test block is placed in an airtight reaction tank body of a kettle type reaction device of the building material carbonization test system, the airtight reaction tank body is vacuumized to negative pressure through a vacuumizing device of the kettle type reaction device, then carbon dioxide gas is rapidly filled into the airtight reaction tank body through a carbon dioxide gas input device of the kettle type reaction device, so that the air pressure in the airtight reaction tank body reaches normal pressure and the carbon dioxide concentration reaches more than 90%, then the temperature, the humidity and the air pressure in the airtight reaction tank body are regulated to reach preset values through a temperature regulating device, a humidity regulating device and an air pressure regulating device of the kettle type reaction device based on detection of a sensor group of the kettle type reaction device, and then the carbon absorption performance of the test block is observed according to a conventional method.\|[0024] In the preferred application of the invention, the application of the building material carbonization test system in consuming carbon dioxide waste gas generated by cement plants or power plants is to use the building material carbonization test system for carbon maintenance of building materials. The specific steps can be as follows: CO of cement kiln flue gas 2 After trapping, carbon dioxide is input into the airtight reaction tank body through the carbon dioxide input device of the building material carbonization test system, the building material is subjected to carbon curing, and the building material is subjected to constant pressure rapid reaction at the pressure of 1bar-15bar interval and normal temperature for 2 hours, so that the curing process is completed. Not only can greatly save maintenance cost, but also the building material can absorb CO 2 The post strength is obviously increased, and the obvious advantage of low carbon benefit can be reflected while the smoke is consumed.\|[0025] In the preferred application of the invention, the application of the building material carbonization test system in consuming carbon dioxide waste gas generated by cement plants or power plants is to use the building material carbonization test system in the study of durability of building materials. The carbonization test system for the building material can accelerate carbonization of a test piece of the building material by improving the temperature and the pressure of the test environment, thereby achieving the purpose of shortening the test period.\|[0026] In the application of the invention, the application of the building material carbonization test system in carbon sequestration in deep ground environment is that the building material carbonization test system is used as a test device for: (1) research on CO of inorganic building materials under high-temperature and high-pressure conditions 2 (2) researching influence of factors such as temperature, pressure and the like on carbonization rules, (3) researching CO under different stratum environments 2 Stable temperature and pressure relationship to promote the carbon sink technology, geological sealing technology or rock efflorescence and CO of inorganic building materials 2 Research on mineralization technology.\|[0027] In a preferred application of the invention, the building material carbonization test system is used for rock weathering or CO 2 The application in mineralization is to use the building material carbonization test system as a test device for simulating accelerated weathering and CO under high temperature and high pressure 2 Mineralization process for research of how to accelerate and enlarge CO 2 Is stable and stable.\|[0028] In the art, it is conventionally considered that the carbon dioxide absorption capacity of concrete needs to be tested in a high pressure state, but the inventors considered that from the principle that carbon dioxide enters and reacts in concrete, a more realistic carbon dioxide absorption capacity of concrete can be obtained by testing in high concentration carbon dioxide gas at normal pressure. On the one hand, the concrete is not easy to breathe, because the binding degree of the cementing material, sand and stones in the concrete is higher after hydration reaction, the higher the strength is, the stronger the inner compactness of the concrete is, and the through holes are hardly formed, so that the outside air is difficult to smoothly diffuse into the inside of the concrete. On the other hand, however, there are numerous blind holes in the concrete, in which air is present, which also acts as a barrier to the penetration of external gases into the interior. In the traditional high-concentration concrete carbonization test, the test condition is high pressure, air in the blind hole is not only not easy to discharge under the existence of external high pressure, but also can be compressed, so that the concentration of carbon dioxide in the blind hole of the concrete test block and the concentration of carbon dioxide outside the blind hole have great difference in the test process, and the external carbon dioxide is not easy to enter the blind hole and is fully absorbed. Although each blind hole has limited space, the overall impact on the carbon absorption capacity of the block will be significant when a large number of distributed blind holes in the block are not capable of sufficiently absorbing carbon dioxide.\|[0029] The testing method adopts the mode of vacuumizing firstly and filling the carbon dioxide later, and before filling the carbon dioxide, the gas in the blind hole in the concrete test block can be well discharged under the negative pressure state, a vacuum body is formed, the carbon dioxide can be easily sucked into the concrete test block after filling and can smoothly permeate into each corner and each hole in the concrete test block, and when the carbon dioxide is filled to reach normal pressure, the concentration of the carbon dioxide in the blind hole in the concrete is basically consistent with the concentration measured by an external sensor. This solves two problems: 1) Carbon dioxide can enter the concrete more easily after negative pressure is formed in the test block, and the absorption rate of the carbon dioxide can be rapidly measured, so that rapid evaluation is realized; 2) The potential safety hazard caused by positive pressure or high pressure can be reduced by testing under normal pressure, and the requirements on the bearing capacity and personnel qualification of laboratory equipment are greatly reduced. The carbonization test is generally carried out in a university or research institution, and if the carbonization test can meet the test requirement of high concentration under normal pressure, the test risk can be greatly reduced.\|[0030] Based on the same principle, the test method disclosed by the invention is also applicable to carbonization tests of other inorganic building materials with porous structures.\|DRAWINGS DESCRIPTION\|[0031] FIG. 1 is a schematic view showing the overall structure of the tank reactor according to example 1.\|[0032] FIGS. 2 and 3 are schematic views showing the overall internal structure of the tank reactor according to example 1, taken from different angles.\|[0033] FIG. 4 is a schematic view showing the overall structure of the carbonization test system for a building material according to example 2.\|INVENTION MODE\|Detailed Description\|[0034] In order that the above-recited objects, features and advantages of the present invention will become more apparent, a more particular description of the invention, briefly summarized below, may be had by way of example only, by reference to the appended drawings.\|[0035] In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, but the present invention may be practiced in other ways other than those described herein, and persons skilled in the art will readily appreciate that the present invention is not limited to the specific embodiments disclosed below.\|[0036] In the following detailed description of the embodiments of the present invention, reference is made to the accompanying drawings, which form a part hereof, and in which is shown by way of illustration only, the scope of the invention is not limited by the claims. In addition, the three-dimensional dimensions of length, width and depth should be included in actual fabrication.\|[0037] Example 1 building Material carbonization test kettle reactor\|A kettle type reaction device for carbonization test of building materials has an integral structure shown in figure 1 and comprises an airtight reaction tank body, wherein one end of a shell 100 of the airtight reaction tank body is provided with a sealing cover 101, and the other end of the shell is provided with a fan wind wheel 102. The top of the housing 100 is provided with a barometer 103, a thermometer 104, a hygrometer 105, an exhaust pipe 106, a carbon dioxide concentration sensor (not shown in the figure), and a safety valve 107. The housing 100 is provided with a carbon dioxide gas input pipe 108, an evacuation pipe 109, a water vapor input pipe 110, and an air or nitrogen gas input pipe 111 on the side. A drain 112 (not shown in fig. 1) is also provided at the bottom of the housing 100.\|[0038] As shown in fig. 2 and 3, the inner container 200 is further sleeved inside the outer shell 100 of the airtight reaction tank body, and a certain gap exists between the outer shell 100 and the inner container 200 and is fixedly connected through a plurality of through connectors 300. The inner container 200 is generally divided into a test block placing area and a gas mixing area, and a semi-closed partition board is arranged in the middle; the test block placing area is internally provided with a test block frame 201, and test blocks can be placed on the test block frame 201. The evacuating tube 109 arranged on the outer shell 100 penetrates into the inner container 200 and is opened in the test block placing area, and the pressure gauge 103, the temperature gauge 104 and the humidity gauge 105 arranged on the outer shell 100 are respectively connected with the pressure sensor, the temperature sensor 203 and the humidity sensor 204 arranged in the test block placing area in the inner container 200. A heating rod 205, a fan cover 206 and a plate heat exchanger 207 are arranged in the gas mixing zone. The carbon dioxide gas input pipe 108, the water vapor input pipe 110, the air input pipe 111, and the liquid discharge pipe 112 provided on the housing 100 are all inserted into the inner container 200 and opened in the gas mixing region.\|[0039] The pressure sensor, the temperature sensor 203 and the humidity sensor 204 are used for directly contacting the gas inside the liner 200; the carbon dioxide concentration sensor can be arranged inside or outside the airtight reaction tank body according to the requirement, and when the temperature of the gas inside the airtight reaction tank body is lower than 50 ℃, the carbon dioxide concentration sensor can be arranged inside and used for directly contacting the gas inside the liner 200; when the temperature of the gas in the airtight reaction tank body is greater than or equal to 50 ℃, the carbon dioxide concentration sensor is arranged outside the airtight reaction tank body and is used for contacting the gas which is collected from the airtight reaction tank body and then subjected to cooling and decompression.\|[0040] When the kettle type reaction device is used for carbonization reaction of building materials, the airtight reaction tank body formed by the shell 100, the sealing cover 101 and the liner 200 can provide an airtight space for accommodating test blocks and keep preset carbon dioxide concentration, temperature, air pressure and humidity environments; the heating rod 205, the fan wind wheel 102 and the plate heat exchanger 207 can be used as temperature adjusting devices for adjusting the temperature of the gas in the inner container 200 of the airtight reaction tank body; in addition, the fan wind wheel 102 can also be used for uniformly mixing the gas in the liner 200 to promote the circulation of the gas in the liner 200; the water vapor input pipe 110, the fan wind wheel 102 and the plate heat exchanger 207 are used as humidity adjusting devices for adjusting the humidity of the gas in the inner container 200 of the airtight reaction tank body; the vacuumizing tube 109, the exhaust tube 106 and the air (or nitrogen) input tube 111 together form an air pressure adjusting device which can be used for adjusting the pressure of the air in the inner container 200 of the airtight reaction tank body; the barometer 103, the thermometer 104, the hygrometer 105 and the carbon dioxide concentration meter form a sensor group together with a pressure sensor, a temperature sensor 203, a humidity sensor 204 and a carbon dioxide concentration sensor which are respectively connected with the barometer 103, the thermometer 104, the hygrometer 105 and the carbon dioxide concentration meter, and the sensor group is used for monitoring the air pressure, the temperature, the humidity and the carbon dioxide concentration in the liner 200; the carbon dioxide gas input pipe 108 is used for externally connecting carbon dioxide storage equipment, and inputting carbon dioxide gas into the inner container 200 of the airtight reaction tank body so as to reach the preset carbon dioxide gas concentration; the drain pipe 112 is used to drain the liquid accumulated at the bottom of the liner 200.\|[0041] Example 2 carbonization test System for building Material\|A carbonization test system for building materials has an overall structure shown in FIG. 4, and comprises a kettle-type reaction device and a control center as described in example 1; the control center is provided with a control cabinet 400, a control circuit board is arranged in the control cabinet 400, and a temperature measurement and control module, a humidity measurement and control module, a pressure measurement and control module, a carbon dioxide concentration measurement and control module, a control circuit and a chip are arranged on the control circuit board. The touch screen 401 capable of performing man-machine interaction is arranged outside the control cabinet 400. Each measurement and control module is electrically connected with a corresponding sensor of the kettle-type reaction device through an electric wire and an electromagnetic valve respectively, receives signals or data from the corresponding sensor, and controls the operation of a fan wind wheel 102, a water vapor input pipe 110, a heating rod 205, a plate heat exchanger 207, a vacuumizing pipe 109, an exhaust pipe 106, an air (or nitrogen) input pipe 111 and a carbon dioxide gas input pipe 108 of the kettle-type reaction device through a control circuit and the electromagnetic valve, so that the airtight reaction tank body of the kettle-type reaction device achieves preset parameter conditions. The touch screen 401 may display a man-machine interaction interface for displaying operation state parameters of the tank reactor to an operator, and for inputting parameters and instructions by the operator; the chip utilizes the embedded program to complete data processing and control of each measurement and control module and the touch screen.\|[0042] The building material carbonization test system of the embodiment has higher safety when being used for high-concentration carbonization test of building materials, the test result is more in accordance with the actual situation, the carbon absorption or carbon resistance of the building materials under the condition of high-concentration carbon dioxide can be measured under normal pressure, and the carbon waste gas generated by cement factories or power plants, carbon fixation of deep environments and rock weathering or CO are consumed 2 The research of mineralization and the like has higher reference value.\|[0043] Example 3 high concentration carbonization test method for building Material\|A high-concentration carbonization testing method for building materials adopts the system of the embodiment 2 of the invention, and comprises the following steps:\|the prepared test blocks of the building material are intensively placed on the test block holder 201 in the liner 200, and then the sealing cover 101 is closed and locked, so that an airtight space is formed inside the liner 200. Before testing, the inside of the inner container 200 of the airtight reaction tank body is vacuumized to negative pressure through the vacuumizing tube 109 of the kettle type reaction device, then the carbon dioxide gas is rapidly filled into the inner container 200 through the carbon dioxide gas input tube 108 on the airtight reaction tank body, so that the air pressure in the inner container 200 of the airtight reaction tank body reaches normal pressure and the carbon dioxide concentration reaches more than 90%, then based on the detection of the pressure sensor, the temperature sensor 203, the humidity sensor 204 and the carbon dioxide concentration sensor, the control center controls the operation of the fan wind wheel 102, the water vapor input tube 110, the heating rod 205, the plate heat exchanger 207, the vacuumizing tube 109, the exhaust tube 106, the air input tube 111 and the carbon dioxide gas input tube 108 according to the embedded programs and algorithms of the chips, so that the temperature, the humidity and the air pressure in the airtight reaction tank body reach preset values, and then the carbon absorption performance of the building material test block is observed according to the conventional method.	Family Number\|(106692037)\|106692037\|Object of Invention\|(CN116808978 A)\|( . . . ) The invention also provides the building material carbonization test system for carbon sequestration and rock weathering or CO in the deep environment consuming carbon dioxide waste gas 2 Mineralization and other research applications . \|The invention relates to a kettle type reaction device capable of providing high - concentration carbon dioxide , which uses carbon dioxide waste gas to carry out inorganic building material maintenance , carbon sequestration in deep environment , rock weathering and CO 2 Mineralization and other research applications . \|Abstract\|(CN116808978 A)\|The invention provides a kettle type reaction device for a carbonization test of a building material . The kettle type reaction device comprises an airtight reaction tank body , a temperature adjusting device , a humidity adjusting device , an air pressure adjusting device , a carbon dioxide gas input device and a sensor group . The invention further provides a building material carbonization test system . The building material carbonization test system comprises the kettle type reaction device and a control center . The invention also provides an application of the building material carbonization test system in researches such as consumption of carbon dioxide waste gas , carbon immobilization in a deep ground environment , rock weathering or CO2 mineralization and the like . The building material carbonization test system disclosed by the invention has higher safety when being used for high - concentration carbonization test of the building material , the test result is more in line with the real situation , and the carbon absorption or carbon resistance of the building material under the condition of high - concentration carbon dioxide can be measured under normal pressure ; the method has higher reference value for research on consumption of carbon dioxide waste gas , carbon immobilization of deep ground environment , rock weathering or CO2 mineralization and the like . \|	Analysis of biological materials\|Chemical engineering\|Other special machines				B01J-019/00\|B01J-019/24\|B28B-011/24\|G01D-021/02\|G01N-033/38	B01J-019/00\|B01J-019/24\|B28B-011/24\|G01D-021/02\|G01N-033/38					CN219092083U\|CN116252380\|CN219111536U\|CN217247947U\|CN206002540U\|KR100686495	CN219092083U 105134867 WHO=Examiner SELF=N CAT=Y CAT=X\|CN116252380 105291149 WHO=Examiner SELF=N CAT=Y\|CN219111536U 105174535 WHO=Examiner SELF=N CAT=A\|CN217247947U 101445038 WHO=Examiner SELF=N CAT=A\|CN206002540U 75611541 WHO=Examiner SELF=N CAT=A\|KR100686495 34004485 WHO=Examiner SELF=N CAT=A		KR100686495; CN219092083U; CN219111536U; CN116252380; CN206002540U; CN217247947U		REVOKED	(CN116808978)\|REVOKED	DEAD	(CN116808978)\|DEAD	(CN116808978)\|LEGAL DETAILS FOR CN116808978\|Actual or expected expiration date=2025-02-21\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2023-07-17\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202310871419\|Application date=2023-07-17\|Standardized application number=2023CN-0871419\|Event publication date=2023-09-29\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN116808978\|Publication stage code=A\|Publication date=2023-09-29\|Standardized publication number=CN116808978\|Event publication date=2023-09-29\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2023-10-24\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2025-02-21\|Event code=CN/RJ01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Rejection of an application after its publication			https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoS5zxZVvzcMc1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000069675907&ekey=2236&xpn=CN116808978&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=vv3VyocLermzgUb19TswmZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN116808978)\|CN	(CN116808978)\|NAME=NELD INTELLIGENT TECHNOLOGY XIANGHE CO., LTD. , COUNTRY=CN		(CN116808978)\|NAME=LIU JUNLING;BEIJING ZHAOJUN UNION INTELLECTUAL PROPERTY LAW FIRM , REG=11333		(CN116808978)\|NAME=ZHANG HUIYI	(CN116808978)\|3	1	1					(CN116808978)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2023-09-29\|Gazette number: GAZNUM=39-3902\|Number of Pages: NPAGES=13\|		(CN116808978)\|CHINESE (CHI)	(CN116808978)\|Patent	Titre: (CN116808978)\|Kettle-type reaction device for carbonization test of building materials and application of kettle-type reaction device Résumé: (CN116808978)\|The invention provides a kettle type reaction device for a carbonization test of a building material. The kettle type reaction device comprises an airtight reaction tank body, a temperature adjusting device, a humidity adjusting device, an air pressure adjusting device, a carbon dioxide gas input device and a sensor group. The invention further provides a building material carbonization test system. The building material carbonization test system comprises the kettle type reaction device and a control center. The invention also provides an application of the building material carbonization test system in researches such as consumption of carbon dioxide waste gas, carbon immobilization in a deep ground environment, rock weathering or CO2 mineralization and the like. The building material carbonization test system disclosed by the invention has higher safety when being used for high-concentration carbonization test of the building material, the test result is more in line with the real situation, and the carbon absorption or carbon resistance of the building material under the condition of high-concentration carbon dioxide can be measured under normal pressure; the method has higher reference value for research on consumption of carbon dioxide waste gas, carbon immobilization of deep ground environment, rock weathering or CO2 mineralization and the like.	23	Abstract	gpt-4o-mini	no	The focus is on carbonization tests of building materials, not on accelerated weathering or CO2 capture through mineral alteration.
24	US05/892,043\|US06/068,316	US06/068,316\|ZA791501\|DK128479\|IT4852779\|JPS54-35156\|EP79400191\|DE2962375T\|AU4533979\|CA322199	CA1124031\|DE2962375\|EP0004807\|AU520262\|US4299805\|ZA791501\|EP0004807\|EP0004807\|JPS54-133498\|AU4533979\|DK128479\|IT7948527	1081365	US4299805 A 1981-11-10 [US4299805]\|ZA791501 B 1980-11-26 [ZA7901501]\|DK128479 A 1979-10-01 [DK7901284]\|IT7948527 A0 1979-03-29 [IT7948527]\|JPS54-133498 A 1979-10-17 [JP54133498]\|EP0004807 B1 1982-03-31 [EP---4807]\|EP0004807 A3 1979-10-31 [EP---4807]\|EP0004807 A2 1979-10-17 [EP---4807]\|DE2962375 D1 1982-05-06 [DE2962375]\|AU520262 B2 1982-01-21 [AU-520262]\|AU4533979 A 1979-10-04 [AU7945339]\|CA1124031 A 1982-05-25 [CA1124031]	1978-03-30\|1979-08-21	1979-08-21\|1979-03-29\|1979-03-29\|1979-03-29\|1979-03-27\|1979-03-26\|1979-03-26\|1979-03-22\|1979-02-23	1982-05-25\|1982-05-06\|1982-03-31\|1982-01-21\|1981-11-10\|1980-11-26\|1979-10-31\|1979-10-17\|1979-10-17\|1979-10-04\|1979-10-01\|1979-03-29	(EP---4807)\|1982-03-31\|(US4299805)\|1981-11-10\|(DE2962375)\|1982-05-06\|\|(CA1124031)\|1982-05-25\|(AU-520262)\|1982-01-21\|(ZA7901501)\|1980-11-26\|\|	(EP0004807)\|1999-03-26\|(US4299805)\|1998-11-10\|(DE2962375)\|1986-12-02\|(JPS54-133498)\|1988-10-17\|(CA1124031)\|1999-05-25\|(AU520262)\|1998-01-21\|(ZA791501)\|1999-03-29\|(DK128479)\|1984-10-01\|(IT7948527)\|1999-03-29	(EP0004807)\|Regeneration of carbon employed in the wet process production of phosphoric acid	(EP0004807)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.	CALGON\|CALGON CARBON\|U	(EP0004807)\|CALGON CORPORATION ([US])\|(EP0004807)\|Calgon Corporation\|(EP0004807)\|CALGON CORPORATION ([US])\|(US4299805)\|Calgon Corporation ([US])\|(DE2962375)\|CALGON CORPORATION\|(JPS54-133498)\|CALGON CORP\|(CA1124031)\|CALGON CORPORATION ([US])\|(AU520262)\|CALGON CORPORATION\|(AU4533979)\|CALGON CORPORATION\|(ZA791501)\|CALGON CORP\|(DK128479)\|CALGON CORPORATION\|(IT7948527)\|CALGON CORPORATION\|U.S.A.	WELLS, BRUCE DOUGLAS\|TIGGELBECK, DONALD DAVID	(EP0004807)\|Wells, Bruce Douglas\|Tiggelbeck, Donald David\|(EP0004807)\|Wells, Bruce Douglas\|Tiggelbeck, Donald David\|(EP0004807)\|Wells, Bruce Douglas\|Tiggelbeck, Donald David	(EP0004807)\|Corre, Jacques Denis Paul;Cabinet Regimbeau ([FR])\|Reg. Nb: 00014911\|(US4299805)\|Katz Martin L.\|Riedl Edmunde D.\|Olson R. Brent\|(CA1124031)\|GOUDREAU, GAGE & ASSOCIATES ([CA])	(EP0004807)\|Generally, the so-called liquid phase activated carbons are preferred since their pore size distribution is sufficiently large to allow for easy access of liquids to the interior of the pores.\|Indeed, the exact nature of the contaminants is difficult to state with precision since the composition of the raw phosphate rock will differ with the run of the mine and even more widely from mine to mine.\|	(EP0004807)\|1. A process for regenerating activated carbon employed for removal of contamination from brown phosphoric acid or aqueous solution of crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by passing aqueous solution comprising 1% to 50% by weight of a base through said activated charcoal and subsequent thereto passing a 0.5 to 2.0N aqueous solution of mineral acid other than brown phosphoric acid through said activated carbon.\|2. In the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1-10 hours; washing the activated carbon with water to remove residual base; contacting the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1-16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|	(EP0004807)\|The present invention is also directed to the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1 to 10 hours; washing the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1 to 16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|This invention relates to an improved process for recycling and regenerating activated carbon employed in the purification of phosphoric acid produced by the wet-process.\|	(EP0004807)\|PHOSPHORIC ACID(100,41)\|BROWN PHOSPHORIC ACID(100,10)\|AQUEOUS SOLUTION(100,9)\|ACTIVATED CARBON REGENERATION(100,6)\|BROWN PHOSPHORIC ACID FILTRATION(100,4)\|ALKALI METAL RAW(100,3)\|CARBON REGENERATION(100,3)\|CRUDE ALKALI METAL PHOSPHATE 3(100,3)\|ALKALI PHOSPHATE 3(100,2)\|PRODUCING PHOSPHORIC ACID(100,2)\|CONTAMINATION REMOVAL(100,1)\|PRODUCING WET(100,1)\|ALKALI TREATMENT(72,3)\|BROWN RESIDUE(72,2)\|RESIDUAL BROWN PHOSPHORIC ACID(63,2)\|ACTIVATED CARBON(50,49)\|MINERAL ACID(41,10)\|PHOSPHORIC ACID PURIFICATION(37,1)\|SEQUENTIAL BATCH(37,1)\|ASH CONTENT(29,1)\|RECYCLING(29,1)\|RESIDUAL ALKALI(29,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(27,1)\|ACTIVATED CHARCOAL(22,2)\|PORE SIZE(20,2)\|ROCK(17,2)\|SODIUM HYDROXIDE(11,2)\|DIGESTION DEBACTEROL(11,1)\|GYPSUM GROSS PARTICLE(11,1)\|PHOSPHATIC FERTILIZER(11,1)\|PHOTOMETRY COLORIMETRY(11,1)\|LIQUID PHASE(9,1)\|LIQUID PHASE ACTIVATED CARBON(9,1)\|PULVERIZE ROCK(9,1)\|THRICE REPEATED DRAINING(9,1)\|ALKANOL AMMONIA(8,1)\|BROWN TINGE(8,1)\|CONTAMINANT VARIED MIX(8,1)\|NEUTRALIZE CRUDE(8,1)\|ROCK IMPURITY(8,1)\|UNDUE DETRIMENT(8,1)\|MARGINAL ARROW(6,1)\|NI TRICE(6,1)\|PETROLEUM ACID SLUDGE(6,1)\|RAW BROWN(6,1)\|TRICKLE BED(6,1)\|VIRGIN CAPACITY(6,1)\|BROWN ACID(5,2)\|GRADE PHOSPHORIC ACID(5,2)\|GREEN PHOSPHORIC ACID(5,2)\|REFILLING(5,2)\|ACTIVATED CARBON INTERMITTENT WASHING(5,1)\|ALKALI CARBONATE(5,1)\|BROWN PRODUCTION(5,1)\|CAUSTIC SOLUTION(5,1)\|COMPLEX SILICATE(5,1)\|ELECTROTHERMAL PHOSPHORIC ACID(5,1)\|ELEMINATED(5,1)\|FLUSHING(5,1)\|GRANULAR CARBON(5,1)\|PAST FOOD(5,1)\|RESIDUAL PHOSPHORIC ACID BULK(5,1)\|ACTIVATED CARBON BED(4,3)\|PATHWAY(4,2)\|ACIDIC WASH(4,1)\|ACTIVATED CARBON PURIFICATION(4,1)\|BACKWASH(4,1)\|BITUMINOUS COAL(4,1)\|CAPITAL INVESTMENT(4,1)\|COMPLETION(4,1)\|CRUSHING(4,1)\|DISPOSAL(4,1)\|EFFLUENT(4,1)\|ELEMENTAL PHOSPHORIC ACID(4,1)\|EXCESS SALT(4,1)\|EXPERIMENTATION(4,1)\|FOOD PRODUCTION(4,1)\|IMPURITE(4,1)\|INFLUX(4,1)\|LIGNITE(4,1)\|NEUTRALIZING(4,1)\|OCCASION(4,1)\|\|(EP0004807)\|PHOSPHORIC ACID(100,41)\|BROWN PHOSPHORIC ACID(100,10)\|AQUEOUS SOLUTION(100,9)\|ACTIVATED CARBON REGENERATION(100,6)\|BROWN PHOSPHORIC ACID FILTRATION(100,4)\|ALKALI METAL RAW(100,3)\|CARBON REGENERATION(100,3)\|CRUDE ALKALI METAL PHOSPHATE 3(100,3)\|ALKALI PHOSPHATE 3(100,2)\|PRODUCING PHOSPHORIC ACID(100,2)\|CONTAMINATION REMOVAL(100,1)\|PRODUCING WET(100,1)\|ALKALI TREATMENT(72,3)\|BROWN RESIDUE(72,2)\|RESIDUAL BROWN PHOSPHORIC ACID(63,2)\|ACTIVATED CARBON(50,49)\|MINERAL ACID(41,10)\|PHOSPHORIC ACID PURIFICATION(37,1)\|SEQUENTIAL BATCH(37,1)\|ASH CONTENT(29,1)\|RECYCLING(29,1)\|RESIDUAL ALKALI(29,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(27,1)\|ACTIVATED CHARCOAL(22,2)\|PORE SIZE(20,2)\|ROCK(17,2)\|SODIUM HYDROXIDE(11,2)\|DIGESTION DEBACTEROL(11,1)\|GYPSUM GROSS PARTICLE(11,1)\|PHOSPHATIC FERTILIZER(11,1)\|PHOTOMETRY COLORIMETRY(11,1)\|LIQUID PHASE(9,1)\|LIQUID PHASE ACTIVATED CARBON(9,1)\|PULVERIZE ROCK(9,1)\|THRICE REPEATED DRAINING(9,1)\|ALKANOL AMMONIA(8,1)\|BROWN TINGE(8,1)\|CONTAMINANT VARIED MIX(8,1)\|NEUTRALIZE CRUDE(8,1)\|ROCK IMPURITY(8,1)\|UNDUE DETRIMENT(8,1)\|MARGINAL ARROW(6,1)\|NI TRICE(6,1)\|PETROLEUM ACID SLUDGE(6,1)\|RAW BROWN(6,1)\|TRICKLE BED(6,1)\|VIRGIN CAPACITY(6,1)\|BROWN ACID(5,2)\|GRADE PHOSPHORIC ACID(5,2)\|GREEN PHOSPHORIC ACID(5,2)\|REFILLING(5,2)\|ACTIVATED CARBON INTERMITTENT WASHING(5,1)\|ALKALI CARBONATE(5,1)\|BROWN PRODUCTION(5,1)\|CAUSTIC SOLUTION(5,1)\|COMPLEX SILICATE(5,1)\|ELECTROTHERMAL PHOSPHORIC ACID(5,1)\|ELEMINATED(5,1)\|FLUSHING(5,1)\|GRANULAR CARBON(5,1)\|PAST FOOD(5,1)\|RESIDUAL PHOSPHORIC ACID BULK(5,1)\|ACTIVATED CARBON BED(4,3)\|PATHWAY(4,2)\|ACIDIC WASH(4,1)\|ACTIVATED CARBON PURIFICATION(4,1)\|BACKWASH(4,1)\|BITUMINOUS COAL(4,1)\|CAPITAL INVESTMENT(4,1)\|COMPLETION(4,1)\|CRUSHING(4,1)\|DISPOSAL(4,1)\|EFFLUENT(4,1)\|ELEMENTAL PHOSPHORIC ACID(4,1)\|EXCESS SALT(4,1)\|EXPERIMENTATION(4,1)\|FOOD PRODUCTION(4,1)\|IMPURITE(4,1)\|INFLUX(4,1)\|LIGNITE(4,1)\|NEUTRALIZING(4,1)\|OCCASION(4,1)\|\|(EP0004807)\|PHOSPHORIC ACID(100,41)\|BROWN PHOSPHORIC ACID(100,10)\|AQUEOUS SOLUTION(100,9)\|ACTIVATED CARBON REGENERATION(100,6)\|BROWN PHOSPHORIC ACID FILTRATION(100,4)\|ALKALI METAL RAW(100,3)\|CARBON REGENERATION(100,3)\|CRUDE ALKALI METAL PHOSPHATE 3(100,3)\|ALKALI PHOSPHATE 3(100,2)\|PRODUCING PHOSPHORIC ACID(100,2)\|CONTAMINATION REMOVAL(100,1)\|PRODUCING WET(100,1)\|ALKALI TREATMENT(72,3)\|BROWN RESIDUE(72,2)\|RESIDUAL BROWN PHOSPHORIC ACID(63,2)\|ACTIVATED CARBON(50,49)\|MINERAL ACID(41,10)\|PHOSPHORIC ACID PURIFICATION(37,1)\|SEQUENTIAL BATCH(37,1)\|ASH CONTENT(29,1)\|RECYCLING(29,1)\|RESIDUAL ALKALI(29,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(27,1)\|ACTIVATED CHARCOAL(22,2)\|PORE SIZE(20,2)\|ROCK(17,2)\|SODIUM HYDROXIDE(11,2)\|DIGESTION DEBACTEROL(11,1)\|GYPSUM GROSS PARTICLE(11,1)\|PHOSPHATIC FERTILIZER(11,1)\|PHOTOMETRY COLORIMETRY(11,1)\|LIQUID PHASE(9,1)\|LIQUID PHASE ACTIVATED CARBON(9,1)\|PULVERIZE ROCK(9,1)\|THRICE REPEATED DRAINING(9,1)\|ALKANOL AMMONIA(8,1)\|BROWN TINGE(8,1)\|CONTAMINANT VARIED MIX(8,1)\|NEUTRALIZE CRUDE(8,1)\|ROCK IMPURITY(8,1)\|UNDUE DETRIMENT(8,1)\|MARGINAL ARROW(6,1)\|NI TRICE(6,1)\|PETROLEUM ACID SLUDGE(6,1)\|RAW BROWN(6,1)\|TRICKLE BED(6,1)\|VIRGIN CAPACITY(6,1)\|BROWN ACID(5,2)\|GRADE PHOSPHORIC ACID(5,2)\|GREEN PHOSPHORIC ACID(5,2)\|REFILLING(5,2)\|ACTIVATED CARBON INTERMITTENT WASHING(5,1)\|ALKALI CARBONATE(5,1)\|BROWN PRODUCTION(5,1)\|CAUSTIC SOLUTION(5,1)\|COMPLEX SILICATE(5,1)\|ELECTROTHERMAL PHOSPHORIC ACID(5,1)\|ELEMINATED(5,1)\|FLUSHING(5,1)\|GRANULAR CARBON(5,1)\|PAST FOOD(5,1)\|RESIDUAL PHOSPHORIC ACID BULK(5,1)\|ACTIVATED CARBON BED(4,3)\|PATHWAY(4,2)\|ACIDIC WASH(4,1)\|ACTIVATED CARBON PURIFICATION(4,1)\|BACKWASH(4,1)\|BITUMINOUS COAL(4,1)\|CAPITAL INVESTMENT(4,1)\|COMPLETION(4,1)\|CRUSHING(4,1)\|DISPOSAL(4,1)\|EFFLUENT(4,1)\|ELEMENTAL PHOSPHORIC ACID(4,1)\|EXCESS SALT(4,1)\|EXPERIMENTATION(4,1)\|FOOD PRODUCTION(4,1)\|IMPURITE(4,1)\|INFLUX(4,1)\|LIGNITE(4,1)\|NEUTRALIZING(4,1)\|OCCASION(4,1)\|\|(US4299805)\|ACTIVATED CARBON(100,63)\|PHOSPHORIC ACID(100,43)\|BROWN PHOSPHORIC ACID(100,12)\|IMPURITY(100,6)\|CARBON REGENERATION(100,2)\|PRODUCING WET(100,1)\|BROWN PHOSPHORIC ACID FILTRATION(92,4)\|BROWN RESIDUE(68,2)\|ALKALI HYDROXIDE(66,5)\|RESIDUAL BROWN PHOSPHORIC ACID(59,2)\|RESIDUAL ALKALI HYDROXIDE(57,1)\|AQUEOUS SOLUTION(55,7)\|RESIDUAL ALKALI(54,3)\|AQUEOUS ALKALI HYDROXIDE(54,1)\|ALKANOL AMMONIA(53,2)\|BROWN PHOSPHORIC ACID PURIFICATION(51,1)\|CAUSTIC CYCLE(50,1)\|DECOLORIZATION(45,1)\|ALKYL AMMONIA(39,2)\|ALKALI CARBONATE(38,2)\|ALKALI HYDROXIDE AQUEOUS SOLUTION(38,1)\|MINERAL ACID DIGESTION(38,1)\|MINERAL ACID(37,10)\|ACID RESIDUE(34,1)\|PHOSPHORIC ACID PURIFICATION(31,1)\|AQUEOUS ALKALI(30,2)\|BASIC AQUEOUS SOLUTION(28,1)\|AMMONIUM HYDROXIDE(24,1)\|RECYCLING(24,1)\|BASE CYCLE(23,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(23,1)\|ACID SOLUTION SEQUENTIAL BATCH(22,1)\|PORE SIZE(17,2)\|AQUEOUS ACID SOLUTION(15,1)\|ROCK(14,2)\|WASHING WATER(14,2)\|ACIDIC SOLUTION(14,1)\|MINERAL ACID SOLUTION(11,1)\|RED FUMING NITRIC ACID(9,2)\|SODIUM HYDROXIDE(9,2)\|DIGESTION DEBACTEROL(9,1)\|GYPSUM GROSS PARTICLE(9,1)\|PHOSPHATIC FERTILIZER(9,1)\|PHOTOMETRY COLORIMETRY(9,1)\|LIQUID PHASE(8,1)\|LIQUID PHASE ACTIVATED CARBON(8,1)\|PULVERIZE ROCK(8,1)\|THRICE REPEATED DRAINING(8,1)\|BROWN TINGE(7,1)\|CONTAMINANT VARIED MIX(7,1)\|NEUTRALIZE CRUDE(7,1)\|ROCK IMPURITY(7,1)\|UNDUE DETRIMENT(7,1)\|WET(5,8)\|MARGINAL ARROW(5,1)\|PETROLEUM ACID SLUDGE(5,1)\|RAW BROWN(5,1)\|TRICKLE BED(5,1)\|VIRGIN CAPACITY(5,1)\|ACTIVATED CARBON BED(4,3)\|BROWN ACID(4,2)\|GRADE PHOSPHORIC ACID(4,2)\|GREEN PHOSPHORIC ACID(4,2)\|PATHWAY(4,2)\|REFILLING(4,2)\|BROWN PRODUCTION(4,1)\|CAUSTIC SOLUTION(4,1)\|COMPLEX SILICATE(4,1)\|ELECTROTHERMAL PHOSPHORIC ACID(4,1)\|FLUSHING(4,1)\|GRANULAR CARBON(4,1)\|PAST FOOD(4,1)\|RESIDUAL PHOSPHORIC ACID BULK(4,1)\|SEPERATION(4,1)\|ACTIVATED CARBON PURIFICATION(3,1)\|BACKWASH(3,1)\|BITUMINOUS COAL(3,1)\|CAPITAL INVESTMENT(3,1)\|COMPLETION(3,1)\|CRUSHING(3,1)\|DISPOSAL(3,1)\|EFFLUENT(3,1)\|ELEMENTAL PHOSPHORIC ACID(3,1)\|EXCESS SALT(3,1)\|EXPERIMENTATION(3,1)\|FOOD PRODUCTION(3,1)\|INFLUX(3,1)\|LIGNITE(3,1)\|NEUTRALIZING(3,1)\|\|(CA1124031)\|ACTIVATED CARBON(100,30)\|PHOSPHORIC ACID(100,14)\|BROWN PHOSPHORIC ACID(100,8)\|ACTIVATED CARBON REGENERATION(100,3)\|ALKALI PHOSPHATE 3(100,3)\|IMPURITY(100,2)\|PRODUCING PHOSPHORIC ACID(100,2)\|PRODUCING WET(100,1)\|BROWN PHOSPHORIC ACID FILTRATION(97,4)\|ALKALI HYDROXIDE(77,4)\|BROWN RESIDUE(71,2)\|ALKANOL AMMONIA(71,1)\|AQUEOUS SOLUTION(66,5)\|BROWN H3PO(65,1)\|RESIDUAL BROWN PHOSPHORIC ACID(62,2)\|RESIDUAL ALKALI HYDROXIDE(60,1)\|RESIDUAL ALKALI(57,3)\|AQUEOUS ALKALI HYDROXIDE(56,1)\|BROWN PHOSPHORIC ACID PURIFICATION(54,1)\|ALKYL AMMONIA(53,1)\|CAUSTIC CYCLE(53,1)\|CRUDE BASE(53,1)\|ALKALI CARBONATE(51,1)\|DECOLORIZATION(48,1)\|MINERAL ACID(44,7)\|AQUEOUS ALKALI(43,1)\|ALKALI HYDROXIDE AQUEOUS SOLUTION(40,1)\|MINERAL ACID DIGESTION(40,1)\|ACID RESIDUE(35,1)\|BASIC AQUEOUS SOLUTION(29,1)\|AMMONIUM HYDROXIDE(25,1)\|ALKALI METAL RAW(24,1)\|BASE CYCLE(24,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(24,1)\|ACID SOLUTION SEQUENTIAL BATCH(23,1)\|DEBACTEROL(23,1)\|WASHING WATER(18,1)\|AQUEOUS ACID SOLUTION(16,1)\|	(EP0004807)\|1. A process for regenerating activated carbon employed for removal of contamination from brown phosphoric acid or aqueous solution of crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by passing aqueous solution comprising 1% to 50% by weight of a base through said activated charcoal and subsequent thereto passing a 0.5 to 2.0N aqueous solution of mineral acid other than brown phosphoric acid through said activated carbon.\|2. In the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1-10 hours; washing the activated carbon with water to remove residual base; contacting the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1-16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|3. A process according to claim 2 where the base is an alkali hydroxide.\|4. A process according to claim 3 where the mineral acid is sulfuric acid.\|5. A process according to claim 3 where the activated carbon is granular.\|6. A process according to claim 3 where the alkali hydroxide is sodium hydroxide.\|7. A process according to claim 3 where the activated carbon is steeped in at least two sequential batches of alkali hydroxide solution.\|8. A process according to claim 3 where the activated carbon is washed with water subsequent to the removal of the mineral acid.\|9. A process according to claim 3 where subsequent to removal of residual alkali hydroxide solution the brown phosphoric acid is filtered through said carbon until its capacity is exhausted, and the activated carbon is washed and treated with the alkali hydroxide.\|10. A regenerated activated carbon having a mesh between 10 and 20 U.S. Standard and an ash content of less than 1 % by weight prepared by the process of claim 1.	(EP0004807)\|Disclosure of the invention:\|[0001] This invention relates to an improved process for recycling and regenerating activated carbon employed in the purification of phosphoric acid produced by the wet-process.\|Background of the invention:\|[0002] In the past food and pharmaceutical grade phosphoric acid or alkali metal phosphates including, for example, trisodium phosphate, sodium tripolyphosphate, tetrasodium pyrophosphate and disodium phosphate were prepared by the thermal acid method described in Slack, Phosphoric Acid, V. 1, pp. 927-966, Marcel Dekker, Inc. (1968). The phosphoric acid and phosphates used in food, pharmaceuticals and in the processing of foods and pharmaceuticals must within stringent limits be substantially free from arsenic, fluorides, heavy metals and general contaminants referred to as insolubles.\|[0003] The thermal process for producing food and pharmaceutical grade phosphoric acid produces extremely pure phosphoric acid, but requires extensive capital investment for equipment, a large input of energy and pollution control equipment. Until recently, the inability to confidently remove contaminants made electrothermal phosphoric acid prepared from elemental phosphorous the predominant source of pure phosphoric acid.\|[0004] The so-called wet process employing phosphate rock and sulfuric acid is well known in the art and described in Waggamen Phosphoric Acid, Phosphates and Phosphatic Fertilizer, pp. 174-209, Hafner Publishing Co. (2nd Ed., 1969). The wet process is also broad enough to include acids other than sulfuric, including nitrice and hydrochloric acid. This is described in Slack, Phosphoric Acid, V. 1, Part 2, pp. 889-926, Marcel Dekker, Inc. (1968).\|[0005] U.S. Patent No. 1,533,031 and French Patent Nos. 1,290,655 and 1,264,118 disclose the regeneration of carbon by base washing followed by acid washing.\|[0006] Many processes were proposed to remove the contaminants found in wet process phosphoric acid and substantially all the successful processes employ activated carbon. For example, see US-A-3,993,733; US-A-3,872,215: US-A-3,993,736; US-A-3,122,415; and GB-A-1,442,919. Unfortunately, the phosphate rock impurities deactivate the porous activated carbon and because sufficient of these impurities are inorganic, thermal regeneration of the activated carbon is unsuitable because phosphate glasses fuse to the pores of the activated carbon. Since the use of activated carbon was the key to so many successful processes for upgrading wet process phosphoric acid, however, some means to increase the life of the too quickly exhausted activated carbon was necessary, since mere disposal after only limited use is clearly economically unsatisfactory. Attempts were made to backwash the activated carbon with poor results. Washing with caustic as in British Patent ,,1103,224 at first seemed a satisfactory solution, but the activated carbon never returns to more than 90% of the immediately previous cycles capacity, so after four regenerations the capacity is reduced to about 66% of the virgin activated carbon and after ten regeneration cycles with caustic alone, the carbon is substantially exhausted.\|[0007] Clearly, unless inordinate quantities of activated carbon are to be employed a more efficient regeneration means is required to not only save the capital cost and operating of renewing the activated carbon, but also the labor employed in replacement.\|[0008] The process of this invention returns the activated carbon to a condition equivalent to its virgin capacity, it achieves the results required to make wet process phosphoric acid the equivalent of thermal elemental phosphoric acid, since processes using activated carbon now become commercially feasible.\|Detailed description of the invention:\|[0009] The nature and content of the impurities that poison the activated charcoal and necessitate its regeneration are only partially understood. They mostly comprise gypsum that continues to precipitate from the brown phosphoric acid. earth waxes, and humic acids together with heavy metal salts, for example, arsenic, lead and the like as well as fluoride salts and complex silicates. Indeed, the exact nature of the contaminants is difficult to state with precision since the composition of the raw phosphate rock will differ with the run of the mine and even more widely from mine to mine. Also, the sulfur employed to produce the sulfuric acid will itself contain various impurities that carry over to poison, clog or otherwise exhaust the activated carbon. In addition, the wearing of the crushing surfaces of processing equipment employed to pulverize the rock can also introduce impurites that appear in the brown acid. Thus, it is all the more remarkable that the process of this invention is useful in regenerating activated carbon containing such a varied mix of contaminants.\|[0010] In the production of brown acid, phosphate containing rock usually predominantly calcium phosphate is pulverized and digested with mineral acid. The rock material is a mixture of overburden, and organic material running through the veins. Generally, in the digestion sulfuric acid is employed which produces large quantities of calcium sulfate. This slowly precipitates as gypsum. Other mineral acids are suitable and on some occasions employed in the production of phosphoric acid. These other mineral acids also produce contaminants and physical deposits similar to those found in the process when sulfuric acid is employed, except of course, gypsum is for the most part absent. Since the principles of the regeneration process of this invention are independent of the acid employed, the process will be exemplified by means of the sulfuric wet process.\|[0011] Referring to the flow chart, the raw brown acid that usually comes from the wet process digestion is about 28% to 34% by weight (expressed in P 205 content). The brown acid is usually put through a separation step to remove gross particles of gypsum and often a solids contact unit clarifyer to further remove residual solids. This intermediate processing can also be employed to neutralize the crude phosphoric acid to alkali metal phosphates.\|[0012] At this point, many producers employ one or more activated carbon purification steps. In the purification, the brown phosphoric acid is by gravity or by pressure filtered through a bed or column of activated carbon. The activated carbon employed can be derived from bituminous coal, lignite, peat, coconut shells, from wood sources or from petroleum acid sludge, or coke and need not have any particular pore size or mesh size. Generally, the so-called liquid phase activated carbons are preferred since their pore size distribution is sufficiently large to allow for easy access of liquids to the interior of the pores. The gas phase activated carbons are suitable but require a slightly longer residence time of the material to be purified. The more preferred activated carbons are granular and have a total surface area of 500-1200 m2/g. One such carbon is sold as SGL Granular Carbon.\|[0013] In most cases, a residence time of from 1/3-3 hours in the activated carbon is satisfactory, while 1 1/2 hours is most desirable. When the existing phosphoric acid is no longer green, but starts to take on a brown tinge or if such a lengthy residence time is required that production is hampered or color specifications are exceeded, it is time to regenerate the carbon.\|[0014] The present invention is also directed to the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1 to 10 hours; washing the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1 to 16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|[0015] In its broadest aspects, the invention entails intermittent washing of the activated carbon with aqueous base and aqueous mineral acid. This acid-base treatment can be sequential or the activated carbon can be employed to filter phosphoric acid between treatment with either acid or base.\|[0016] The regeneration of the activated carbon is, however, preferably performed in accordance with the steps 1-17 set forth in the table. In the preferred process, the column or bed of activated carbon is drained of its contents and refilled with whatever solution is dictated by the next step, and that solution allowed to steep in the column or bed of activated carbon for the specified time usually from 1-10 hours, before proceeding to the next step. If plant conditions dictate it is, however, suitable to practice continuous influx and outflow, during all steps, if this continuous flusing is practical rather than the "drain-fill steep" preferred embodiment the contact time of water, base and acid, should be adjusted accordingly so they are equivalent to the residence time set forth in the preferred embodiment.\|[0017] It should be noted that a number of steps in the preferred process can suitably be eliminated without undue detriment to the activated carbon. These eleminated steps are indicated by the marginal arrows for example from step 2b to step 9a. Otherwise, it is generally preferred to follow the steps in sequence.\|[0018] Proceeding from step 11, when the green acid produced starts to show more than the desired level of contamination, the activated carbon bed or column is removed from service drained and filled with water as in step 1 a. After a contact time of from 1/4 to about 4 hours, the column or bed is drained, step 1 b, preferably collecting the effluent which is enriched in phosphoric acid. This water washing sequence is repeated as in steps 2a through 3b. As already stated a continuous flow water wash is nearly as satisfactory. What is desired is that the bulk of residual phosphoric acid is flushed from the activated carbon so that neutralization producing excess salts that could deteriorate the activated carbon does not occur when the caustic solution is employed.\|[0019] Then in step 4a, the activated carbon bed or column is loaded with a 1% to 50% by weight aqueous solution of base. By the term "base" it is meant a substance that in aqueous solution induces a pH of 8 and preferably 10. Suitable bases include alkali hydroxides, alkali carbonates, ammonia, lower alkylamines and lower alkanol amines. The preferred base is sodium hydroxide. This solution is allowed to remain in the bed or column for from 1/4 to 10 hours. The base solution is then drained from the bed or column. This can be repeated one or more times, but is not absolutely required.\|[0020] Again, a continuous flow for 1/4 to 10 hours such as in a trickle bed is satisfactory, but the steeping is preferred. The caustic is then rinsed from the bed or column as in step 7a in the same manner as in steps 1-3. While, one water wash is sufficient, it is preferred at least three water washings be employed.\|[0021] At this point, the bed or column can be either returned to operation step 10 or treated with the acid as in step 12 and as set forth below in detail. If returned to operation, the cycle steps 1-11 are repeated from 1 to 8 additional times or until the specification for the phosphoric acid shows by photometry colorimetry or other analytical means that excessive impurities are present in the green phosphoric acid. At that point, the activated carbon bed or column is then treated with acid subsequent to the water rinse following the caustic steep. The column or bed is filled with from 0.5 to 2ZN . aqueous mineral acid such as sulfuric, hydrochloric, or nitric acid although sulfuric acid is preferred. This solution is allowed to steep in the carbon bed or column for from 1/2 to 16 hours. A single fill without draining and refilling is generally preferred but a twice or thrice repeated draining and refilling is suitable, but not found to be necessary in most cases. The acid steep as all other operations in steps 1-17 is preferably conducted at ambient temperature, but temperatures from 20°C. to 60°C. are suitable. When the temperature exceeds 25°C. the time to conduct the regeneration is shortened proportionately and from 1-4 hours is in most cases found sufficient.\|[0022] The exact time period, of course, must be determined by some experimentation because of the wide variation in the chemical composition of phosphate rock raw material. After completing steps 12b, 13b or 14b where the spent acid is conveniently channeled to the rock digestion process, the activated carbon is preferably water washed as in steps 1-3 or by continuous flow as previously described. The water wash can be eliminated but this is not at all recommended since the green phosphoric acid becomes contaminated with sulfuric acid. This may, however, be satisfactory when fertilizer grade phosphoric acid is contemplated.\|[0023] The activated carbon obtained from the process of this invention after the caustic-rinse acid-rinse cycle steps 1-17 is novel in that it comprises an activated carbon having a surprisingly low ash, generally less than 1% as indicated by ASTM D-2866-70. The novel activated carbon is also characterized in that the size range of the activated carbon particles is substantially uniform and is within a range of 10-20 mesh U.S. Standard. This carbon being so uniquely low in ash and of a substantially uniform size is particularly suitable for operations where such properties are desirable as in the filtration of pharmaceutical products or intermediates.\|[0024] In the attached flow sheet, the solid lines indicate the most usual pathway in the production of wet process phosphoric acid. The dashed lines indicate optional pathways which may be employed by various users of the wet process without departing from the spirit or scope of this invention.\|TABLE 1\|	(EP0004807)\|Disclosure of the invention:\|[0001] This invention relates to an improved process for recycling and regenerating activated carbon employed in the purification of phosphoric acid produced by the wet-process.\|Background of the invention:\|[0002] In the past food and pharmaceutical grade phosphoric acid or alkali metal phosphates including, for example, trisodium phosphate, sodium tripolyphosphate, tetrasodium pyrophosphate and disodium phosphate were prepared by the thermal acid method described in Slack, Phosphoric Acid, V. 1, pp. 927-966, Marcel Dekker, Inc. (1968). The phosphoric acid and phosphates used in food, pharmaceuticals and in the processing of foods and pharmaceuticals must within stringent limits be substantially free from arsenic, fluorides, heavy metals and general contaminants referred to as insolubles.\|[0003] The thermal process for producing food and pharmaceutical grade phosphoric acid produces extremely pure phosphoric acid, but requires extensive capital investment for equipment, a large input of energy and pollution control equipment. Until recently, the inability to confidently remove contaminants made electrothermal phosphoric acid prepared from elemental phosphorous the predominant source of pure phosphoric acid.\|[0004] The so-called wet process employing phosphate rock and sulfuric acid is well known in the art and described in Waggamen Phosphoric Acid, Phosphates and Phosphatic Fertilizer, pp. 174-209, Hafner Publishing Co. (2nd Ed., 1969). The wet process is also broad enough to include acids other than sulfuric, including nitrice and hydrochloric acid. This is described in Slack, Phosphoric Acid, V. 1, Part 2, pp. 889-926, Marcel Dekker, Inc. (1968).\|[0005] U.S. Patent No. 1,533,031 and French Patent Nos. 1,290,655 and 1,264,118 disclose the regeneration of carbon by base washing followed by acid washing.\|[0006] Many processes were proposed to remove the contaminants found in wet process phosphoric acid and substantially all the successful processes employ activated carbon. For example, see US-A-3,993,733; US-A-3,872,215: US-A-3,993,736; US-A-3,122,415; and GB-A-1,442,919. Unfortunately, the phosphate rock impurities deactivate the porous activated carbon and because sufficient of these impurities are inorganic, thermal regeneration of the activated carbon is unsuitable because phosphate glasses fuse to the pores of the activated carbon. Since the use of activated carbon was the key to so many successful processes for upgrading wet process phosphoric acid, however, some means to increase the life of the too quickly exhausted activated carbon was necessary, since mere disposal after only limited use is clearly economically unsatisfactory. Attempts were made to backwash the activated carbon with poor results. Washing with caustic as in British Patent ,,1103,224 at first seemed a satisfactory solution, but the activated carbon never returns to more than 90% of the immediately previous cycles capacity, so after four regenerations the capacity is reduced to about 66% of the virgin activated carbon and after ten regeneration cycles with caustic alone, the carbon is substantially exhausted.\|[0007] Clearly, unless inordinate quantities of activated carbon are to be employed a more efficient regeneration means is required to not only save the capital cost and operating of renewing the activated carbon, but also the labor employed in replacement.\|[0008] The process of this invention returns the activated carbon to a condition equivalent to its virgin capacity, it achieves the results required to make wet process phosphoric acid the equivalent of thermal elemental phosphoric acid, since processes using activated carbon now become commercially feasible.\|Detailed description of the invention:\|[0009] The nature and content of the impurities that poison the activated charcoal and necessitate its regeneration are only partially understood. They mostly comprise gypsum that continues to precipitate from the brown phosphoric acid. earth waxes, and humic acids together with heavy metal salts, for example, arsenic, lead and the like as well as fluoride salts and complex silicates. Indeed, the exact nature of the contaminants is difficult to state with precision since the composition of the raw phosphate rock will differ with the run of the mine and even more widely from mine to mine. Also, the sulfur employed to produce the sulfuric acid will itself contain various impurities that carry over to poison, clog or otherwise exhaust the activated carbon. In addition, the wearing of the crushing surfaces of processing equipment employed to pulverize the rock can also introduce impurites that appear in the brown acid. Thus, it is all the more remarkable that the process of this invention is useful in regenerating activated carbon containing such a varied mix of contaminants.\|[0010] In the production of brown acid, phosphate containing rock usually predominantly calcium phosphate is pulverized and digested with mineral acid. The rock material is a mixture of overburden, and organic material running through the veins. Generally, in the digestion sulfuric acid is employed which produces large quantities of calcium sulfate. This slowly precipitates as gypsum. Other mineral acids are suitable and on some occasions employed in the production of phosphoric acid. These other mineral acids also produce contaminants and physical deposits similar to those found in the process when sulfuric acid is employed, except of course, gypsum is for the most part absent. Since the principles of the regeneration process of this invention are independent of the acid employed, the process will be exemplified by means of the sulfuric wet process.\|[0011] Referring to the flow chart, the raw brown acid that usually comes from the wet process digestion is about 28% to 34% by weight (expressed in P 205 content). The brown acid is usually put through a separation step to remove gross particles of gypsum and often a solids contact unit clarifyer to further remove residual solids. This intermediate processing can also be employed to neutralize the crude phosphoric acid to alkali metal phosphates.\|[0012] At this point, many producers employ one or more activated carbon purification steps. In the purification, the brown phosphoric acid is by gravity or by pressure filtered through a bed or column of activated carbon. The activated carbon employed can be derived from bituminous coal, lignite, peat, coconut shells, from wood sources or from petroleum acid sludge, or coke and need not have any particular pore size or mesh size. Generally, the so-called liquid phase activated carbons are preferred since their pore size distribution is sufficiently large to allow for easy access of liquids to the interior of the pores. The gas phase activated carbons are suitable but require a slightly longer residence time of the material to be purified. The more preferred activated carbons are granular and have a total surface area of 500-1200 m2/g. One such carbon is sold as SGL Granular Carbon.\|[0013] In most cases, a residence time of from 1/3-3 hours in the activated carbon is satisfactory, while 1 1/2 hours is most desirable. When the existing phosphoric acid is no longer green, but starts to take on a brown tinge or if such a lengthy residence time is required that production is hampered or color specifications are exceeded, it is time to regenerate the carbon.\|[0014] The present invention is also directed to the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1 to 10 hours; washing the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1 to 16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|[0015] In its broadest aspects, the invention entails intermittent washing of the activated carbon with aqueous base and aqueous mineral acid. This acid-base treatment can be sequential or the activated carbon can be employed to filter phosphoric acid between treatment with either acid or base.\|[0016] The regeneration of the activated carbon is, however, preferably performed in accordance with the steps 1-17 set forth in the table. In the preferred process, the column or bed of activated carbon is drained of its contents and refilled with whatever solution is dictated by the next step, and that solution allowed to steep in the column or bed of activated carbon for the specified time usually from 1-10 hours, before proceeding to the next step. If plant conditions dictate it is, however, suitable to practice continuous influx and outflow, during all steps, if this continuous flusing is practical rather than the "drain-fill steep" preferred embodiment the contact time of water, base and acid, should be adjusted accordingly so they are equivalent to the residence time set forth in the preferred embodiment.\|[0017] It should be noted that a number of steps in the preferred process can suitably be eliminated without undue detriment to the activated carbon. These eleminated steps are indicated by the marginal arrows for example from step 2b to step 9a. Otherwise, it is generally preferred to follow the steps in sequence.\|[0018] Proceeding from step 11, when the green acid produced starts to show more than the desired level of contamination, the activated carbon bed or column is removed from service drained and filled with water as in step 1 a. After a contact time of from 1/4 to about 4 hours, the column or bed is drained, step 1 b, preferably collecting the effluent which is enriched in phosphoric acid. This water washing sequence is repeated as in steps 2a through 3b. As already stated a continuous flow water wash is nearly as satisfactory. What is desired is that the bulk of residual phosphoric acid is flushed from the activated carbon so that neutralization producing excess salts that could deteriorate the activated carbon does not occur when the caustic solution is employed.\|[0019] Then in step 4a, the activated carbon bed or column is loaded with a 1% to 50% by weight aqueous solution of base. By the term "base" it is meant a substance that in aqueous solution induces a pH of 8 and preferably 10. Suitable bases include alkali hydroxides, alkali carbonates, ammonia, lower alkylamines and lower alkanol amines. The preferred base is sodium hydroxide. This solution is allowed to remain in the bed or column for from 1/4 to 10 hours. The base solution is then drained from the bed or column. This can be repeated one or more times, but is not absolutely required.\|[0020] Again, a continuous flow for 1/4 to 10 hours such as in a trickle bed is satisfactory, but the steeping is preferred. The caustic is then rinsed from the bed or column as in step 7a in the same manner as in steps 1-3. While, one water wash is sufficient, it is preferred at least three water washings be employed.\|[0021] At this point, the bed or column can be either returned to operation step 10 or treated with the acid as in step 12 and as set forth below in detail. If returned to operation, the cycle steps 1-11 are repeated from 1 to 8 additional times or until the specification for the phosphoric acid shows by photometry colorimetry or other analytical means that excessive impurities are present in the green phosphoric acid. At that point, the activated carbon bed or column is then treated with acid subsequent to the water rinse following the caustic steep. The column or bed is filled with from 0.5 to 2ZN . aqueous mineral acid such as sulfuric, hydrochloric, or nitric acid although sulfuric acid is preferred. This solution is allowed to steep in the carbon bed or column for from 1/2 to 16 hours. A single fill without draining and refilling is generally preferred but a twice or thrice repeated draining and refilling is suitable, but not found to be necessary in most cases. The acid steep as all other operations in steps 1-17 is preferably conducted at ambient temperature, but temperatures from 20°C. to 60°C. are suitable. When the temperature exceeds 25°C. the time to conduct the regeneration is shortened proportionately and from 1-4 hours is in most cases found sufficient.\|[0022] The exact time period, of course, must be determined by some experimentation because of the wide variation in the chemical composition of phosphate rock raw material. After completing steps 12b, 13b or 14b where the spent acid is conveniently channeled to the rock digestion process, the activated carbon is preferably water washed as in steps 1-3 or by continuous flow as previously described. The water wash can be eliminated but this is not at all recommended since the green phosphoric acid becomes contaminated with sulfuric acid. This may, however, be satisfactory when fertilizer grade phosphoric acid is contemplated.\|[0023] The activated carbon obtained from the process of this invention after the caustic-rinse acid-rinse cycle steps 1-17 is novel in that it comprises an activated carbon having a surprisingly low ash, generally less than 1% as indicated by ASTM D-2866-70. The novel activated carbon is also characterized in that the size range of the activated carbon particles is substantially uniform and is within a range of 10-20 mesh U.S. Standard. This carbon being so uniquely low in ash and of a substantially uniform size is particularly suitable for operations where such properties are desirable as in the filtration of pharmaceutical products or intermediates.\|[0024] In the attached flow sheet, the solid lines indicate the most usual pathway in the production of wet process phosphoric acid. The dashed lines indicate optional pathways which may be employed by various users of the wet process without departing from the spirit or scope of this invention.\|TABLE 1\|	Family Number\|(1081365)\|1081365\|Object of Invention\|(CA1124031 A)\|Abstract of the Disclosure In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali (...) \|(EP---4807 A3)\|In a process tor regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali (...) \|(EP---4807 A2)\|In a process tor regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali (...) \|(US4299805 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3 PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali (...) \|Abstract\|(AU-520262 B2)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(CA1124031 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrocloric, or nitric acid, again washed with water to remove residual acid and returned to service. Usually, the acid steep need not be employed with every base cycle to maintain good decolorization, although if desired the acid steep can be used with each caustic cycle.\|(DE2962375 D1)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(DK7901284 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(EP---4807 B1)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.\|(IT7948527 A0)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(JP54133498 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(US4299805 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitric acid, again washed with water to remove residual acid and returned to service. Usually, the acid steep need not be employed with every base cycle to maintain good decolorization, although if desired the acid steep can be used with each caustic cycle.\|(ZA7901501 B)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|Independent Claims\|(EP---4807 B1)\|1. A process for regenerating activated carbon employed for removal of contamination from brown phosphoric acid or aqueous solution of crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by passing aqueous solution comprising 1% to (...) \|(EP---4807 A2)\|1. A process for regenerating activated carbon employed for removal of contamination from brown phosphoric acid or aqueous solution of crude alkali metal phosphates derived therefrom comprising passing aqueous solution comprising 1% to 50% by weight of a base through said activated charcoal and subsequent thereto (...) \|	Chemical engineering\|Materials, metallurgy	C01B-025/235\|C01B-025/30/8\|C01B-032/36		C01B-025/235\|C01B-025/30/8\|C01B-032/36	B01J-020/34\|C01B-025/234\|C01B-025/235\|C01B-025/30\|C01B-031/08	B01J-020/34\|C01B-025/16\|C01B-025/22\|C01B-025/234\|C01B-025/235\|C01B-025/30\|C01B-031/08\|C01B-031/12	PCLO=423321100	PCLO=423321000R PCLX=252412000	WO200579977\|CN102417178\|WO200066490\|CN117160184\|CN116395689\|CN113713762\|CN113247895\|CN113247895\|CN103896267\|US20100111811\|US20060223701\|CN116585848B\|US20070060476\|US7569514\|US7119047\|DE4222524\|US4822765\|US4761284\|US4558022\|US4495165\|US4503022\|US4407725\|US4407725	WO200579977 44555513 WHO=Examiner SELF=N CAT=Y\|CN102417178 7612130 WHO=Examiner SELF=N CAT=X\|WO200066490 1420164 WHO=Examiner SELF=N CAT=X\|CN117160184 107597685 WHO=Examiner SELF=N CAT=A\|CN116395689 105666606 WHO=Examiner SELF=N CAT=A\|CN113713762 97352655 WHO=Examiner SELF=N CAT=A\|CN113247895 95650355 WHO=Examiner SELF=N CAT=A\|CN113247895 95650355 WHO=Examiner SELF=N CAT=A\|CN103896267 66514074 WHO=Examiner SELF=N CAT=A\|US20100111811 15025702 WHO=Examiner SELF=N CAT=103\|US20060223701 43493001 WHO=Examiner SELF=N CAT=103\|CN116585848B 106130958 WHO=Examiner SELF=N\|US20070060476 43493001 WHO=Examiner SELF=N\|US7569514 43493001 WHO=Applicant SELF=N\|US7119047 43493001 WHO=Examiner SELF=N\|DE4222524 13017496 WHO=Examiner SELF=N\|US4822765 42614360 WHO=Examiner SELF=N\|US4761284 42614360 WHO=Examiner SELF=N\|US4558022 198388 WHO=Examiner SELF=Y\|US4495165 14627359 WHO=Examiner SELF=N\|US4503022 42527050 WHO=Examiner SELF=N\|US4407725 42501230 WHO=Examiner SELF=N\|US4407725 42501230 WHO=Examiner SELF=N	GB1103224\|FR2234228\|US3186793\|US3944513\|DE2206706\|US3720626\|GB1103224\|FR1290665\|GB-934695\|US1533031\|FR-481511	GB1103224 2259233 WHO=Examiner SELF=N CAT=A CAT=D\|FR2234228 12450784 WHO=Examiner SELF=N CAT=A\|US3186793 41868616 WHO=Examiner SELF=N CAT=A\|US3944513 42279640 WHO=Examiner SELF=N\|DE2206706 12367549 WHO=Examiner SELF=N\|US3720626 2339106 WHO=Examiner SELF=N\|GB1103224 2259233 WHO=Examiner SELF=N\|FR1290665 16545164 WHO=Examiner SELF=N\|GB-934695 17766161 WHO=Examiner SELF=N\|US1533031 40387123 WHO=Examiner SELF=N\|FR-481511 15856956 WHO=Examiner SELF=N		FR1290665; GB1103224; US3720626; US3944513\|\|\|\|\|DE2206706; US1533031; FR-481511; GB-934695; GB1103224; US3186793; FR2234228\|\|\|	(EP0004807)\|Search Report references [Examiner]\|-CHEMICAL ABSTRACTS, Vol. 87, no. 24, 12 December 1977 Abstract no. 188820r, page 267, column 1 Columbus, (Ohio), USA, M. BECCARI et al.: "Chemical regeneration of granular activated carbon" & EFFLUENT WATER TREATMENT JOURNAL 17 (6) 1977, pages 287, 290-295.\|-JOURNAL OF APPLIED CHEMISTRY OF THE USSR, Vol. 51, no. 8, part 1, August 1978, New York, USA, N.A. YAKUBENYA et al.: "Regeneration of active carbon used for purification of waste gases during production of synthetic fibers", pages 1683-1685.\|\|\|\|\|\|\|\|\|	EXPIRED	(EP0004807)\|EXPIRED\|(US4299805)\|EXPIRED\|(DE2962375)\|LAPSED\|(JPS54-133498)\|LAPSED\|(CA1124031)\|EXPIRED\|(AU520262)\|EXPIRED\|(ZA791501)\|EXPIRED\|(DK128479)\|LAPSED\|(IT7948527)\|LAPSED	DEAD	(EP0004807)\|DEAD\|(US4299805)\|DEAD\|(DE2962375)\|DEAD\|(JPS54-133498)\|DEAD\|(CA1124031)\|DEAD\|(AU520262)\|DEAD\|(ZA791501)\|DEAD\|(DK128479)\|DEAD\|(IT7948527)\|DEAD	(EP0004807)\|LEGAL DETAILS FOR EP0004807\|Actual or expected expiration date=1999-03-26\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-03-26\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP79400191\|Application date=1979-03-26\|Standardized application number=1979EP-0400191\|Event publication date=1979-08-21\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=1979-09-03\|Event code=EP/PUAL\|Event group=Examination events\|SEARCH REPORT DESPATCHED\|Publication of search report\|Original code: 0009013\|Event publication date=1979-10-17\|Event code=EP/A2\|Event group=Examination events\|Application published without search report\|Publication country=EP\|Publication number=EP0004807\|Publication stage code=A2\|Publication date=1979-10-17\|Standardized publication number=EP---4807\|Event publication date=1979-10-17\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=BE CH DE FR GB LU NL SE\|Event publication date=1979-10-31\|Event code=EP/A3\|Event indicator=Pos\|Event group=Examination events\|Published search report\|Publication country=EP\|Publication number=EP0004807\|Publication stage code=A3\|Publication date=1979-10-31\|Standardized publication number=EP---4807\|Event publication date=1979-10-31\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=BE CH DE FR GB LU NL SE\|Event publication date=1980-03-05\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Event publication date=1982-01-30\|Event code=EP/GRAA\|Event indicator=Pos\|Event group=Examination events\|(EXPECTED) GRANT\|Original code: 0009210\|Event publication date=1982-03-31\|Event code=EP/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent specification\|Publication country=EP\|Publication number=EP0004807\|Publication stage code=B1\|Publication date=1982-03-31\|Standardized publication number=EP---4807\|Event publication date=1982-03-31\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=BE CH DE FR GB LU NL SE\|Event publication date=1982-07-12\|Event code=EP/KL\|Event group=Corrections\|Correction list\|82/04\|Event publication date=1999-03-26\|Event code=EP/EEDX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent has expired\|Event publication date=2016-09-14\|Event code=EP/PLBE\|Event indicator=Pos\|Event group=No opposition filed\|NO OPPOSITION FILED WITHIN TIME LIMIT\|Original code: 0009261\|Event publication date=2016-09-14\|Event code=EP/STAANOPP\|Event indicator=Pos\|Event group=No opposition filed Event indicating In Force\|No opposition filed within time limit\|Original code: STAA\|MEMBER STATE LEGAL DETAILS FOR BE\|Actual or expected expiration date=1986-03-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BE\|Event publication date=1984-12-31\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1984-12-31\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=BE\|Event publication date=1986-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=BE\|Event publication date=1986-09-30\|Event code=EP/BERE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|BE: Lapsed\|BE: Dechu\|OWNER:CALGON CARBON CORP.\|Effective date of the event=1986-03-31\|Corresponding cc:\|Designated or member state=BE\|MEMBER STATE LEGAL DETAILS FOR CH\|Actual or expected expiration date=1984-03-31\|Legal state=DEAD\|Status=EXPIRED\|Corresponding cc:\|Designated or member state=CH\|Event publication date=1983-01-31\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1983-01-31\|Year of payment of annual fees=5\|Corresponding cc:\|Designated or member state=CH\|Event publication date=1984-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=CH\|Event publication date=1984-11-30\|Event code=EP/REG\|Event code=CH/PL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent ceased\|Loeschung/radiation/radiazion\|Corresponding cc:\|Designated or member state=CH\|MEMBER STATE LEGAL DETAILS FOR DE2962375\|Actual or expected expiration date=1986-12-02\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE Corresponding appl: DE2962375\|Application date in the designated or member state=1979-03-26\|Application number in the designated or member state=1979DE-2962375\|Corresponding cc:\|Designated or member state=DE Corresponding pat: DE2962375\|Publication stage code in the designated or member state=D1\|Publication date in the designated or member state=1982-05-06\|Publication number in the designated or member state=DE2962375\|Event publication date=1982-05-06\|Event code=EP/REF\|Event group=Entry into national phase\|Corresponds to:\|Corresponding cc:\|Designated or member state=DE\|Event publication date=1984-01-31\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1984-01-31\|Year of payment of annual fees=6\|Corresponding cc:\|Designated or member state=DE\|Event publication date=1986-12-02\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR FR\|Actual or expected expiration date=1986-11-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=FR\|Event publication date=1984-11-29\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1984-11-29\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=FR\|Event publication date=1985-12-27\|Event code=EP/REG\|Event code=FR/CD\|Event group=Change of name or address Reassignment\|Reference to a national code\|Change of name or company name\|Changement de nom de denomination\|Corresponding cc:\|Designated or member state=FR\|Event publication date=1986-11-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=FR\|Event publication date=1987-01-23\|Event code=EP/REG\|Event code=FR/ST\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Notification of lapse\|Constatation de decheances\|Corresponding cc:\|Designated or member state=FR\|MEMBER STATE LEGAL DETAILS FOR GB\|Actual or expected expiration date=1986-11-12\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GB\|Event publication date=1986-11-12\|Event code=EP/GBPC\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|GB: European patent ceased through non-payment of renewal fee\|Corresponding cc:\|Designated or member state=GB\|Event publication date=1988-11-17\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=GB\|MEMBER STATE LEGAL DETAILS FOR LU\|Actual or expected expiration date=1983-03-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LU\|Event publication date=1982-12-22\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1982-12-22\|Year of payment of annual fees=5\|Corresponding cc:\|Designated or member state=LU\|Event publication date=1983-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LU\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=1983-10-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NL\|Event publication date=1983-10-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=NL\|Event publication date=1983-11-16\|Event code=EP/NLV4\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|NL: Lapsed or anulled due to non-payment of the annual fee\|NL: Vervallen wegens niet betalen van een jaarcijns\|Corresponding cc:\|Designated or member state=NL\|MEMBER STATE LEGAL DETAILS FOR SE\|Actual or expected expiration date=1987-02-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SE Corresponding appl: SE79400191.7\|Event publication date=1984-03-31\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1984-03-31\|Year of payment of annual fees=6\|Corresponding cc:\|Designated or member state=SE\|Event publication date=1986-03-27\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=SE\|Event publication date=1995-01-31\|Event code=EP/EUG\|Event indicator=Neg\|Event group=Event indicating Not In Force\|SE: European patent has lapsed\|SE: Europeiskt patent har upphoert att gaella\|Effective date of the event=1987-02-23\|Corresponding cc:\|Designated or member state=SE\|(US4299805)\|LEGAL DETAILS FOR US4299805\|Actual or expected expiration date=1998-11-10\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-08-21\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US06068316\|Application date=1979-08-21\|Standardized application number=1979US-06068316\|Event publication date=1979-08-21\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:HELLER, GREGORY\|Event publication date=1979-08-21\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1103\|Event publication date=1979-08-21\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: C1193CA\|Event publication date=1979-08-21\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: UNDISCOUNTED\|Event publication date=1979-08-21\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=1980-02-06\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=1980-02-06\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=1981-05-08\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=1981-05-08\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=1981-07-21\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=1981-07-21\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST.\|Assignors:TIGGELBECK DONALD D;WELLS BRUCE D.\|Reel/frame:003884/0398\|OWNER:CALGON CORPORATION ROUTE 60 & CAMPBELLS RUN RD. RO\|Effective date of the event=1978-03-28\|Event publication date=1981-07-21\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:TIGGELBECK DONALD D;WELLS BRUCE D.\|Reel/frame:003884/0398\|OWNER:CALGON CORPORATION ROUTE 60 & CAMPBELLS RUN RD. RO\|Effective date of the event=1978-03-28\|Event publication date=1981-11-06\|Event code=US/N066\|Event group=Payment or non-payment notifications\|Notice of balance of issue fee due (pto-1031) - charged to deposit account\|Event publication date=1981-11-10\|Event code=US/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Patents Granted before 2001-04-15\|Publication country=US\|Publication number=US04299805\|Publication stage code=A\|Publication date=1981-11-10\|Standardized publication number=US4299805\|Event publication date=1981-11-10\|Event code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=1984-12-21\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|CHANGE OF NAME\|Assignor:CALGON CORPORATION\|Reel/frame:004345/0918\|OWNER:CALGON CARBON CORPORATION\|Effective date of the event=1982-06-24\|Event publication date=1985-05-01\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|SECURITY INTEREST\|Assignor:CALGON CARBON CORPORATION\|Reel/frame:004398/0398\|OWNER:BANKERS TRUST COMPANY\|Effective date of the event=1985-04-19\|Event publication date=1989-01-09\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|RELEASED BY SECURED PARTY\|Assignor:BANKERS TRUST COMPANY\|Reel/frame:005017/0627\|OWNER:CALGON CARBON CORPORATION\|Effective date of the event=1988-09-01\|Event publication date=1998-11-10\|Event code=US/EEDX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent has expired\|(DE2962375)\|LEGAL DETAILS FOR DE2962375\|Actual or expected expiration date=1986-12-02\|Legal state=DEAD\|Status=LAPSED\|Event publication date=1979-03-26\|Event code=DE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=DE DE2962375\|Application date=1979-03-26\|Standardized application number=1979DE-2962375\|Event publication date=1982-05-06\|Event code=DE/D1\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant (no unexamined application published) patent law 81\|Patenterteilung (keine 0s) patg. 81\|Publication country=DE\|Publication number=DE2962375\|Publication stage code=D1\|Publication date=1982-05-06\|Standardized publication number=DE2962375\|Event publication date=1986-12-02\|Event code=DE/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Event publication date=1987-03-19\|Event code=DE/8339\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Ceased/non-payment of the annual fee\|Wegen nichtz. d. jahresgeb. erloschen\|(JPS54-133498)\|LEGAL DETAILS FOR JPS54-133498\|Actual or expected expiration date=1988-10-17\|Legal state=DEAD\|Status=LAPSED\|Event publication date=1979-03-27\|Event code=JP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=JP JP3515679\|Application date=1979-03-27\|Standardized application number=1979JP-0035156\|Event publication date=1979-10-17\|Event code=JP/A\|Event group=Examination events\|Published application\|Publication country=JP\|Publication number=JPS54133498\|Publication stage code=A\|Publication date=1979-10-17\|Standardized publication number=JP54133498\|Event publication date=1988-10-17\|Event code=JP/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(CA1124031)\|LEGAL DETAILS FOR CA1124031\|Actual or expected expiration date=1999-05-25\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-02-23\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA322199\|Application date=1979-02-23\|Standardized application number=1979CA-0322199\|Event publication date=1982-05-25\|Event code=CA/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent granted\|Publication country=CA\|Publication number=CA1124031\|Publication stage code=A\|Publication date=1982-05-25\|Standardized publication number=CA1124031\|Event publication date=1999-05-25\|Event code=CA/MKEX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Expiry\|(AU520262)\|LEGAL DETAILS FOR AU520262\|Actual or expected expiration date=1998-01-21\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-03-22\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU4533979\|Application date=1979-03-22\|Standardized application number=1979AU-0045339\|Event publication date=1979-10-04\|Event code=AU/A\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU4533979\|Publication stage code=A\|Publication date=1979-10-04\|Standardized publication number=AU7945339\|Event publication date=1982-01-21\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent preceeded by A1\|Publication country=AU\|Publication number=AU520262\|Publication stage code=B2\|Publication date=1982-01-21\|Standardized publication number=AU-520262\|Event publication date=1999-03-22\|Event code=AU/EEDX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent has expired\|(ZA791501)\|LEGAL DETAILS FOR ZA791501\|Actual or expected expiration date=1999-03-29\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-03-29\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA791501\|Application date=1979-03-29\|Standardized application number=1979ZA-0001501\|Event publication date=1980-11-26\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA791501\|Publication stage code=B\|Publication date=1980-11-26\|Standardized publication number=ZA7901501\|Event publication date=1999-03-29\|Event code=ZA/EEDX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent has expired\|(DK128479)\|LEGAL DETAILS FOR DK128479\|Actual or expected expiration date=1984-10-01\|Legal state=DEAD\|Status=LAPSED\|Event publication date=1979-03-29\|Event code=DK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=DK DK128479\|Application date=1979-03-29\|Standardized application number=1979DK-0001284\|Event publication date=1979-10-01\|Event code=DK/A\|Event group=Examination events\|Published application\|Publication country=DK\|Publication number=DK128479\|Publication stage code=A\|Publication date=1979-10-01\|Standardized publication number=DK7901284\|Event publication date=1984-10-01\|Event code=DK/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IT7948527)\|LEGAL DETAILS FOR IT7948527\|Actual or expected expiration date=1999-03-29\|Legal state=DEAD\|Status=LAPSED\|Event publication date=1979-03-29\|Event code=IT/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IT IT4852779\|Application date=1979-03-29\|Standardized application number=1979IT-0048527\|Event publication date=1979-03-29\|Event code=IT/A0\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=IT\|Publication number=IT7948527\|Publication stage code=A0\|Publication date=1979-03-29\|Standardized publication number=IT7948527\|Event publication date=1999-03-29\|Event code=IT/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned	(EP0004807)\|Contracting States: DE, SE, BE, CH, LU, GB, FR, NL		https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=Ha67aj7xeb/nOPB6GlyZ+WkyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP0000000000059790&ekey=2273&xpn=EP---4807&kind=B1	https://register.epo.org/application?number=EP79400191	https://permalink.orbit.com/RenderStaticFirstPage?XPN=NVVyZEDoMGrdGqGyRhNS9XfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(US4299805)\|US\|\|(EP0004807)\|US\|(EP0004807)\|US\|(CA1124031)\|US	(US4299805)\|NAME=Calgon Corporation , CITY=Pittsburgh , STATE=PA , COUNTRY=US , ATYP=US Company\|(IT7948527)\|NAME=CALGON CORPORATION A ROBINSON TOWNSHIP PENNSYLVANIA\|(EP0004807)\|NAME=CALGON CORPORATION Route 60-Campbell's Run Road , CITY=Robinson TownshipPennsylvania 15205 , COUNTRY=US , REG=00212230\|(EP0004807)\|NAME=CALGON CORPORATION Route 60-Campbell's Run Road , CITY=Robinson TownshipPennsylvania 15205 , COUNTRY=US , REG=00212230\|(CA1124031)\|NAME=CALGON CORPORATION 5400 Campbells Run Road , CITY=PITTSBURGH , STATE=PA , POSTCODE=15205 , COUNTRY=US	(EP0004807)\|FR\|(EP0004807)\|FR\|(EP0004807)\|FR\|\|(CA1124031)\|CA	(EP0004807)\|NAME=Corre, Jacques Denis Paul;Cabinet Regimbeau 26, Avenue Kléber , CITY=75116 Paris , COUNTRY=FR , REG=00014911\|(EP0004807)\|NAME=Corre, Jacques Denis Paul, et al Cabinet Regimbeau 26, Avenue Kléber F-75116 Paris , COUNTRY=FR\|(EP0004807)\|NAME=Corre, Jacques Denis Paul;Cabinet Regimbeau 26, Avenue Kléber , CITY=75116 Paris , COUNTRY=FR , REG=00014911\|(US4299805)\|NAME=Katz Martin L. NAME=Riedl Edmunde D. NAME=Olson R. Brent\|(CA1124031)\|NAME=GOUDREAU, GAGE & ASSOCIATES , COUNTRY=CA	(EP0004807)\|US; US\|\|(EP0004807)\|US; US\|(US4299805)\|US\|\|\|(CA1124031)\|US; US\|\|\|\|	(EP0004807)\|NAME=Wells, Bruce Douglas 74 Mayfair Drive, CITY=PittsburghPennsylvania 15228, COUNTRY=US \|NAME=Tiggelbeck, Donald David 204 Seneca Drive, CITY=PittsburghPennsylvania 15228, COUNTRY=US\|(EP0004807)\|NAME=Wells, Bruce Douglas\|NAME=Tiggelbeck, Donald David\|(EP0004807)\|NAME=Wells, Bruce Douglas 74 Mayfair Drive, CITY=PittsburghPennsylvania 15228, COUNTRY=US \|NAME=Tiggelbeck, Donald David 204 Seneca Drive, CITY=PittsburghPennsylvania 15228, COUNTRY=US\|(US4299805)\|NAME=Wells Bruce D., CITY=Pittsburgh, STATE=PA , COUNTRY=US\|(DE2962375)\|NAME=WELLS, BRUCE DOUGLAS\|NAME=TIGGELBECK, DONALD DAVID\|(JPS54-133498)\|NAME=BURUUSU DAGURASU UERUSU\|NAME=DONARUDO DEIBUITSUDO TEIGERUBE\|(CA1124031)\|NAME=WELLS, BRUCE D., COUNTRY=US \|NAME=TIGGELBECK, DONALD D., COUNTRY=US\|(AU520262)\|NAME=B.D. WELLS\|NAME=D.D. TIGGELBECK\|(AU4533979)\|NAME=BRUCE DOUGLAS WELLS\|NAME=DONALD DAVID TIGGELBECK\|(ZA791501)\|NAME=TIGGELBECK D\|NAME=WELLS B\|(DK128479)\|NAME=WELLS B D\|NAME=TIGGELBECK D D	(US4299805)\|2\|\|	2	9		BANKERS TRUST; FROM 1985-04-19; TO 1988-09-01		(DE2962375)\|EP79400191	(EP0004807)\|Number of Claims: NCL=10\|\|(EP0004807)\|Number of Claims: NCL=10\|\|(US4299805)\|Number of Claims: NCL=14\|Number of Drawings: NDR=2\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1,2\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: Vertiz O. R.\|Art Unit.: ART =113\|\|(CA1124031)\|Number of Claims: NCL=14\|\|(ZA791501)\|Number of Claims: NCL=1\|		(EP0004807)\|ENGLISH (ENG)	(CA1124031)\|Patent\|(DE2962375)\|Patent\|(EP---4807)\|Patent\|(AU-520262)\|Patent\|(US4299805)\|Patent\|(ZA7901501)\|Patent\|(EP---4807)\|Patent\|(EP---4807)\|Patent\|(JP54133498)\|Patent\|(AU7945339)\|Patent\|(DK7901284)\|Patent\|(IT7948527)\|Patent	Titre: (EP0004807)\|Regeneration of carbon employed in the wet process production of phosphoric acid Résumé: (EP0004807)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.	22	Abstract	gpt-4o-mini	no	The article focuses on the regeneration of activated carbon in the production of phosphoric acid, which does not relate to accelerated weathering or CO₂ capture.
25	CN202110935649	CN202110935649	CN113683197	97182255	CN113683197 A 2021-11-23 [CN113683197]	2021-08-16	2021-08-16	2021-11-23		(CN113683197)\|2023-06-23	(CN113683197)\|Efficient nitrogen and phosphorus removal anti-blocking constructed wetland system	(CN113683197)\|The invention discloses an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system, and relates to the technical field of constructed wetland construction. The system comprises an aeration reoxygenation chamber, an enhanced carbon removal chamber, an enhanced nitrogen removal chamber, an enhanced phosphorus removal chamber, a sludge sedimentation tank and the like. A water inlet channel is mainly used for uniformly distributing water and collecting purified water. The aeration reoxygenation chamber is a main body unit for water quality purification and mainly comprises an aeration device, composite filler and plants, and when a polluted water body flows through the unit module, the water quality can be purified by virtue of the composite filler, soil filtration, and activities of aquatic plants, high-efficiency microorganisms and the like. According to the water quality of inlet water and the water quality target needing to be achieved, different concentrated and matched fillers can be selected, so that the enhanced carbon removal chamber, the enhanced nitrogen removal chamber, the enhanced phosphorus removal chamber and the sludge sedimentation tank which are designed and obtained can effectively remove nitrogen, phosphorus, heavy metal, impurity sludge and the like in the water body.	ANHUI XINYU ECOLOGICAL INDUSTRY	(CN113683197)\|ANHUI XINYU ECOLOGICAL IND CO LTD ([CN])	ZHANG YOUDE\|HE JIANJUN\|DAI CAOPEI\|ZHANG TIANTIAN	(CN113683197)\|ZHANG YOUDE\|HE JIANJUN\|DAI CAOPEI\|ZHANG TIANTIAN	(CN113683197)\|WANG XIAOJUN;Hefei Daozhi Intellectual Property Agency Co., Ltd.\|Reg. Nb: 34130	(CN113683197)\|However, the conventional subsurface flow constructed wetland has insufficient dissolved oxygen and the denitrification effect is difficult to meet the strict emission standard, so the current challenges are to effectively balance the oxygen demand and input in the artificial system under the condition of reducing the cost and how to design a system which can ensure the treatment efficiency and keep the system simple and economic in the aspects of layout, construction and maintenance.\|	(CN113683197)\|1. An efficient nitrogen and phosphorus removal anti-blocking constructed wetland system is characterized by comprising an aeration reoxygenation chamber (1), an enhanced decarbonization chamber (2), an enhanced denitrification chamber (3) and an enhanced phosphorus removal chamber (4), wherein a water inlet channel (5) is arranged on the front side of the aeration reoxygenation chamber (1), an observation chamber (6) is arranged between the enhanced decarbonization chamber (2) and the enhanced denitrification chamber (3), and a water drainage channel (7) is arranged on the rear side of the enhanced phosphorus removal chamber (4);the water inlet channel (5) is communicated with the aeration reoxygenation chamber (1) through a first overflow pipe (9), a main pipe (10) and branch pipes are arranged below the aeration reoxygenation chamber (1), and the outer end of the main pipe (10) is connected with an aeration device;a first composite filler (12) is filled in the aeration reoxygenation chamber (1), the first composite filler (12) comprises at least two of large-particle-size crushed stone, gravel, volcanic rock and suspended ceramsite, and the suspended ceramsite contains immobilized microorganisms;the enhanced decarbonization chamber (2) is positioned at the rear side of the aeration reoxygenation chamber (1) and is communicated with the aeration reoxygenation chamber through a second overflow pipe (13), a second composite filler (14) is filled in the enhanced decarbonization chamber (2), and the second composite filler (14) comprises gravel, broken stone and limestone;the enhanced denitrification chamber (3) is positioned at the rear side of the observation chamber (6), a third overflow pipe (15) and a first reserved water pipe (16) are respectively arranged at two sides of the observation chamber (6), the third overflow pipe (15) is communicated with the enhanced decarbonization chamber (2) and the observation chamber (6), the first reserved water pipe (16) is arranged at the bottom and is communicated with the observation chamber (6) and the enhanced denitrification chamber (3); a third composite filler (17) is filled in the enhanced denitrification chamber (3), and the third composite filler (17) comprises gravel, biochar and broken stone;the enhanced phosphorus removal chamber (4) is positioned at the rear side of the enhanced nitrogen removal chamber (3), the enhanced phosphorus removal chamber (4) is communicated with the enhanced nitrogen removal chamber (3) through a fourth overflow pipe (18), a fourth composite filler (19) is filled in the enhanced phosphorus removal chamber, the fourth composite filler (19) comprises gravel, zeolite, coal ash and crushed stone, and the enhanced phosphorus removal chamber (4) is communicated with the drainage channel (7) through a second reserved water pipe (20) arranged at the bottom;the bottom of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced dephosphorization chamber (4) is of a slope structure, a plurality of sludge discharge pipes (26) are pre-buried at the bottoms of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced dephosphorization chamber (4), the sludge discharge pipes (26) are laid on the slope, a plurality of holes are formed in the sludge discharge pipes (26) side by side along the length direction of the pipes, a first stainless steel wire mesh matched with the shape of the sludge discharge pipes is arranged at an orifice, and the mesh size of the first stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding chamber; a sludge discharge groove (27) is formed in the lower side of the slope structure, the lower end of a sludge discharge pipe (26) is connected to the sludge discharge groove (27), the gradient of the bottom of the long side of the sludge discharge groove (27) is set to be 2% -3%, a second stainless steel wire mesh matched with the sludge discharge groove in shape is covered above the sludge discharge groove (27), and the mesh size of the second stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding cavity; mud discharging branch pipes (28) are reserved in the wetland side walls corresponding to the mud discharging grooves (27), and the outer ends of the mud discharging branch pipes (28) are connected with a mud discharging main pipe (29) together.\|	(CN113683197)\|Aiming at the problems in the prior art, the invention provides an artificial wetland ecological restoration process. In order to achieve the purpose, the invention is realized by the following technical scheme:\|The invention discloses an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system, which relates to the technical field of constructed wetland construction and comprises an aeration reoxygenation chamber, an enhanced decarbonization chamber, an enhanced nitrogen removal chamber, an enhanced phosphorus removal chamber, a sludge sedimentation tank and the like.\|The invention relates to the technical field of sewage treatment, in particular to an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system.\|	(CN113683197)\|AERATION REOXYGENATION CHAMBER(100,39)\|CONSTRUCTED WETLAND(100,20)\|PHOSPHORUS REMOVAL(100,12)\|NITROGEN(100,11)\|COMPOSITE FILLER(75,37)\|ENHANCED DECARBONIZATION CHAMBER(65,23)\|ENHANCED DENITRIFICATION CHAMBER(61,26)\|SLUDGE DISCHARGE PIPE(58,8)\|ENHANCED PHOSPHORUS REMOVAL CHAMBER(49,9)\|PHOSPHORUS REMOVAL CHAMBER(47,11)\|OBSERVATION CHAMBER(35,17)\|MICROORGANISM IMMOBILIZATION(35,8)\|MUD DISCHARGE(34,1)\|SLUDGE SEDIMENTATION TANK(33,9)\|ENHANCED DEPHOSPHORIZATION CHAMBER(31,16)\|SUSPENDED CERAMSITE(30,6)\|ARTIFICIAL WETLAND ECOLOGICAL RESTORATION(30,1)\|BRANCH PIPE(29,15)\|SLUDGE(28,28)\|AERATION REOXYGENATION CHAMBER BOTTOM(28,10)\|NITROGEN REMOVAL CHAMBER(27,3)\|ENHANCED NITROGEN REMOVAL CHAMBER(26,3)\|SLUDGE SETTLING TANK(25,13)\|DENITRIFICATION(21,2)\|ANTIBLOCKING CONSTRUCTED WETLAND(20,2)\|GRAVEL(19,10)\|BROKEN ROCK(19,7)\|SLUDGE DISCHARGE GROOVE(19,3)\|FILLER CENTRALIZATION(19,2)\|OVERFLOW PIPE(18,23)\|SUPERNATANT OUTLET(17,4)\|WATER INLET(16,22)\|AERATION(16,5)\|MUD SEDIMENTATION TANK(16,1)\|RESERVING WATER PIPE(15,11)\|CRUSHED STONE(15,5)\|ECOLOGICAL RESTORATION(15,1)\|SLOPE(13,12)\|EARTH FILTRATION(13,2)\|INSUFFICIENT DISSOLVED OXYGEN(13,1)\|STRICT EMISSION STANDARD(13,1)\|SLOPE STRUCTURE(12,6)\|GRADIENT(12,5)\|UPPER COVERING SOIL(12,2)\|COAL ASH(12,1)\|CONSTRUCTED WETLAND CONSTRUCTION(12,1)\|MUD(11,16)\|LIMESTONE(11,3)\|VOLCANIC ROCK(11,3)\|AERATION MAIN PIPE(11,2)\|BIOCHAR(11,2)\|SEPARATION NET(11,1)\|WATER DRAINAGE CHANNEL(10,3)\|DESIGNED ENHANCED DECARBONIZATION CHAMBER(10,2)\|ORIFICE(10,2)\|ARTIFICIAL WETLAND(9,6)\|REINFORCED DENITRIFICATION CHAMBER(9,6)\|POWER MUD(9,5)\|REINFORCED DEPHOSPHORIZATION CHAMBER(9,4)\|ZEOLITE(9,3)\|LAYOUT(9,1)\|DISTRIBUTION(8,2)\|OXYGEN DEMAND(8,1)\|SUBSURFACE FLOW CONSTRUCTED WETLAND(8,1)\|STAINLESS STEEL WIRE MESH(7,9)\|DRAINAGE CHANNEL(7,5)\|UPPER GRAVEL LAYER(7,5)\|SEWAGE TREATMENT(7,4)\|MUD PUMP(7,3)\|SLUDGE DISCHARGE VALVE(7,3)\|STRENGTHENING DECARBONIZATION CHAMBER(7,2)\|MINIMUM PARTICLE SIZE(6,5)\|AQUATIC PLANT(6,4)\|PURIFIED WATER COLLECTION(6,2)\|UNIT MODULE(6,2)\|DTG IMMOBILIZED MICROORGANISM(6,1)\|MESH SIZE(5,6)\|FILLER COMPOUND(5,5)\|INLET WATER(5,2)\|PURIFYING WATER QUALITY(5,2)\|REINFORCED DECARBONIZATION CHAMBER(5,2)\|SUBSURFACE FLOW(5,2)\|ACCUMULATED IMPURITY SLUDGE(5,1)\|AFFORESTATION VEGETATION(5,1)\|INTENSIFIED DECARBONIZATION CHAMBER(5,1)\|THREE LAYER NYLON NET(4,5)\|MUD OUTER END(4,3)\|SUPERNATANT DELIVERY PORT(4,2)\|GREEN VEGETATION(4,1)\|SLUDGE GATHERING TANK(4,1)\|WETLAND BLOCKING PHENOMENON(4,1)\|HIGH EFFICIENCY NITROGEN(3,3)\|INCLINED PLANE(3,3)\|MUD PIPE(3,3)\|LENGTH DIRECTION(3,2)\|REINFORCED PHOSPHORUS REMOVAL CHAMBER(3,2)\|SLUDGE SIDE(3,2)\|AERATION PIPELINE(3,1)\|AERATION ROLE(3,1)\|ENHANCED DENITRIFICATION(3,1)\|GATHERING MUD GROOVE(3,1)\|HIGH EFFICIENCY DENITRIFICATION(3,1)\|MICROBIAL DECOMPOSITION(3,1)\|SLUDGE SETTLING TANK LATERAL(3,1)\|SOIL TRIPLE SYNERGISTIC ACTION(3,1)\|TRANSPIRATION MOISTURE(3,1)\|WETLAND SLUDGE(3,1)\|OUTER END(2,6)\|COVER PLATE(2,3)\|WETLAND SIDE WALL(2,3)\|HEAVY METAL(2,2)\|POWER SLUDGE(2,2)\|CHAMBER TANK(2,1)\|DEPHOSPHORIZATION ARTIFICIAL WETLAND(2,1)\|GROUND COVER(2,1)\|INSULATION(2,1)\|MUD DISCHARGE MAIN PIPE(2,1)\|MUD VALVE(2,1)\|NUTRIENT ABSORPTION(2,1)\|NYLON NET LAYER(2,1)\|OBSERVATION ROOM(2,1)\|OVERFLOW TUBE(2,1)\|PLANT ROOT ADSORPTION(2,1)\|PLANT SHIELDING(2,1)\|PREBURIED MANY MUD(2,1)\|RESIDUE ACCUMULATION(2,1)\|RURAL SEWAGE TREATMENT(2,1)\|SEWAGE PLANT DEEP TREATMENT(2,1)\|SEWAGE TREATMENT DECENTRALIZATION(2,1)\|SLUDGE DISCHARGE MAIN PIPE(2,1)\|SLUDGE PUMP(2,1)\|SLUDGE SETTLING TANK OUTSIDE(2,1)\|SUBSTANCE SUSPENSION(2,1)\|UPPER STRATA EARTHING(2,1)\|WATER INLET INTERCOMMUNICATION(2,1)\|WETLAND PURIFICATION AREA(2,1)\|LONG SIDE(1,2)\|ANIMAL(1,1)\|APRON(1,1)\|ARTIFICIAL CONSTRUCTION MODE(1,1)\|ARTIFICIAL MEDIUM(1,1)\|ARTIFICIAL WETLAND DESIGN(1,1)\|DETENTION(1,1)\|DRILL WAY DEPARTMENT(1,1)\|	(CN113683197)\|1. An efficient nitrogen and phosphorus removal anti-blocking constructed wetland system is characterized by comprising an aeration reoxygenation chamber (1), an enhanced decarbonization chamber (2), an enhanced denitrification chamber (3) and an enhanced phosphorus removal chamber (4), wherein a water inlet channel (5) is arranged on the front side of the aeration reoxygenation chamber (1), an observation chamber (6) is arranged between the enhanced decarbonization chamber (2) and the enhanced denitrification chamber (3), and a water drainage channel (7) is arranged on the rear side of the enhanced phosphorus removal chamber (4);\|the water inlet channel (5) is communicated with the aeration reoxygenation chamber (1) through a first overflow pipe (9), a main pipe (10) and branch pipes are arranged below the aeration reoxygenation chamber (1), and the outer end of the main pipe (10) is connected with an aeration device;\|a first composite filler (12) is filled in the aeration reoxygenation chamber (1), the first composite filler (12) comprises at least two of large-particle-size crushed stone, gravel, volcanic rock and suspended ceramsite, and the suspended ceramsite contains immobilized microorganisms;\|the enhanced decarbonization chamber (2) is positioned at the rear side of the aeration reoxygenation chamber (1) and is communicated with the aeration reoxygenation chamber through a second overflow pipe (13), a second composite filler (14) is filled in the enhanced decarbonization chamber (2), and the second composite filler (14) comprises gravel, broken stone and limestone;\|the enhanced denitrification chamber (3) is positioned at the rear side of the observation chamber (6), a third overflow pipe (15) and a first reserved water pipe (16) are respectively arranged at two sides of the observation chamber (6), the third overflow pipe (15) is communicated with the enhanced decarbonization chamber (2) and the observation chamber (6), the first reserved water pipe (16) is arranged at the bottom and is communicated with the observation chamber (6) and the enhanced denitrification chamber (3); a third composite filler (17) is filled in the enhanced denitrification chamber (3), and the third composite filler (17) comprises gravel, biochar and broken stone;\|the enhanced phosphorus removal chamber (4) is positioned at the rear side of the enhanced nitrogen removal chamber (3), the enhanced phosphorus removal chamber (4) is communicated with the enhanced nitrogen removal chamber (3) through a fourth overflow pipe (18), a fourth composite filler (19) is filled in the enhanced phosphorus removal chamber, the fourth composite filler (19) comprises gravel, zeolite, coal ash and crushed stone, and the enhanced phosphorus removal chamber (4) is communicated with the drainage channel (7) through a second reserved water pipe (20) arranged at the bottom;\|the bottom of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced dephosphorization chamber (4) is of a slope structure, a plurality of sludge discharge pipes (26) are pre-buried at the bottoms of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced dephosphorization chamber (4), the sludge discharge pipes (26) are laid on the slope, a plurality of holes are formed in the sludge discharge pipes (26) side by side along the length direction of the pipes, a first stainless steel wire mesh matched with the shape of the sludge discharge pipes is arranged at an orifice, and the mesh size of the first stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding chamber; a sludge discharge groove (27) is formed in the lower side of the slope structure, the lower end of a sludge discharge pipe (26) is connected to the sludge discharge groove (27), the gradient of the bottom of the long side of the sludge discharge groove (27) is set to be 2% -3%, a second stainless steel wire mesh matched with the sludge discharge groove in shape is covered above the sludge discharge groove (27), and the mesh size of the second stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding cavity; mud discharging branch pipes (28) are reserved in the wetland side walls corresponding to the mud discharging grooves (27), and the outer ends of the mud discharging branch pipes (28) are connected with a mud discharging main pipe (29) together.\|2. The high-efficiency nitrogen and phosphorus removal anti-blocking constructed wetland system of claim 1, a water inlet (8) is arranged on one side of the water inlet channel (5), a sludge sedimentation tank (32) is arranged at the output end of the sludge discharge main pipe (29), a cover plate (33) is arranged at the top of the sludge sedimentation tank (32), a supernatant outlet (34) is arranged on the side part of the sludge sedimentation tank (32), the supernatant outlet (34) is communicated with the water inlet (8), a sludge gathering groove (35) is arranged in the middle of the bottom of the sludge settling tank (32), the bottoms of the sludge settling tank (32) at two sides of the sludge gathering groove (35) are inclined planes with certain gradient, one side close to the sludge gathering groove (35) is a low side, a mud pump (36) is arranged in the mud gathering groove (35), the mud pump (36) is connected with a power mud conveying pipe (37), and the output end of the power mud conveying pipe (37) extends to the outer side of the mud sedimentation tank (32).\|3. The efficient nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 2, wherein the slope of the slopes on two sides of the bottom of the sludge settling tank (32) is 2%.\|4. The high-efficiency nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, characterized in that a support (11) is laid under the aeration main pipe (10) and the branch pipes, and the end of the support (11) is fixedly connected to the bottom of the aeration reoxygenation chamber (1).\|5. The high-efficiency denitrification and dephosphorization anti-blocking constructed wetland system according to claim 1, wherein the immobilized microorganisms are preferably DTG immobilized microorganisms.\|6. The efficient nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, wherein the thicknesses of the first composite filler (12), the second composite filler (14), the third composite filler (17) and the fourth composite filler (19) are controlled to be 10-50 mm, a lower gravel layer (21) with the thickness of 60-100 mm is arranged at the bottom of each layer of composite filler, an upper gravel layer (22) with the thickness of 5-10 mm is arranged at the top of each layer of composite filler, a three-layer nylon net (23) is arranged at the top of the upper gravel layer (22), upper covering soil (24) is laid at the top of the three-layer nylon net (23), and greening vegetation (25) is arranged on the upper covering soil (24).\|7. The efficient nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, wherein the slope of the slope structures at the bottoms of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced phosphorus removal chamber (4) is 2%.\|8. The denitrification and dephosphorization anti-blocking constructed wetland system according to claim 1, wherein the sludge discharge pipe (26) and the sludge discharge groove (27) are vertically connected in spatial position.\|9. The efficient nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, characterized in that sludge discharge valves (30) are independently arranged on the sludge discharge branch pipes (28), and a main valve (30) is arranged on the sludge discharge main pipe (29).\|10. The high-efficiency nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, characterized in that a separation net (38) is arranged above the water inlet channel (5), the observation chamber (6) and the water drainage channel (7).	(CN113683197)\|TECHNICAL FIELD\|[0001] The invention relates to the technical field of sewage treatment, in particular to an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system.\|BACKGROUND ART\|[0002] The artificial wetland is a technology for treating sewage and sludge by using the physical, chemical and biological triple synergistic action of soil, artificial medium, plants and microorganisms in the process of flowing along a certain direction by using sewage and sludge which are controllably dosed to the artificially constructed wetland from the artificially constructed and controlled-operation ground similar to the marshland. The action mechanism of the plant nutrient solution comprises the actions of adsorption, detention, filtration, oxidation reduction, precipitation, microbial decomposition, transformation, plant shielding, residue accumulation, transpiration moisture and nutrient absorption and various animals.\|[0003] However, the conventional subsurface flow constructed wetland has insufficient dissolved oxygen and the denitrification effect is difficult to meet the strict emission standard, so the current challenges are to effectively balance the oxygen demand and input in the artificial system under the condition of reducing the cost and how to design a system which can ensure the treatment efficiency and keep the system simple and economic in the aspects of layout, construction and maintenance. And because the suspended substances in the sewage are intercepted and the biological membranes on the surface of the substrate are accumulated and shed, the artificial wetland is easy to block in the actual operation.\|DISCLOSURE\|Disclosure of Invention\|[0004] Aiming at the problems in the prior art, the invention provides an artificial wetland ecological restoration process.\|[0005] In order to achieve the purpose, the invention is realized by the following technical scheme:\|[0006] an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system comprises an aeration reoxygenation chamber, a reinforced decarbonization chamber, a reinforced denitrification chamber and a reinforced phosphorus removal chamber, wherein a water inlet channel is arranged on the front side of the aeration reoxygenation chamber, an observation chamber is arranged between the reinforced decarbonization chamber and the reinforced denitrification chamber, and a water drainage channel is arranged on the rear side of the reinforced phosphorus removal chamber; the water inlet channel is communicated with the aeration reoxygenation chamber through a first overflow pipe, a main pipe and a branch pipe are arranged below the aeration reoxygenation chamber, and the outer end of the main pipe is connected with an aeration device; filling a first composite filler in the aeration reoxygenation chamber, wherein the first composite filler comprises at least two of large-particle-size crushed stone, gravel, volcanic rock and suspended ceramsite, and the suspended ceramsite contains immobilized microorganisms; the strengthening decarbonization chamber is positioned at the rear side of the aeration reoxygenation chamber and is communicated with the aeration reoxygenation chamber through a second overflow pipe, and second composite fillers are filled in the strengthening decarbonization chamber and comprise gravels, broken stones and limestone; the enhanced denitrification chamber is positioned at the rear side of the observation chamber, a third overflow pipe and a first reserved water pipe are respectively arranged at two sides of the observation chamber, the third overflow pipe is communicated with the enhanced decarbonization chamber and the observation chamber, and the first reserved water pipe is arranged at the bottom and is communicated with the observation chamber and the enhanced denitrification chamber; a third composite filler is filled in the enhanced denitrification chamber, and comprises gravels, charcoal and broken stones; the reinforced dephosphorization chamber is positioned at the rear side of the reinforced denitrification chamber, the reinforced dephosphorization chamber is communicated with the reinforced denitrification chamber through a fourth overflow pipe, a fourth composite filler is filled in the reinforced dephosphorization chamber, the fourth composite filler comprises gravel, zeolite, fly ash and broken stone, and the reinforced dephosphorization chamber is communicated with the drainage channel through a second reserved water pipe arranged at the bottom;\|[0007] the bottom of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber is of a slope structure, a plurality of sludge discharge pipes are pre-buried at the bottoms of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber and laid on the slope, a plurality of holes are arranged in the sludge discharge pipes side by side along the length direction of the pipes, a first stainless steel wire mesh matched with the shape of the first stainless steel wire mesh is arranged at an orifice, and the mesh size of the first stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding chamber; a mud discharging groove is formed in the lower side of the slope structure, the lower end of the mud discharging pipe is connected to the mud discharging groove, the gradient of the bottom of the long side of the mud discharging groove is set to be 2% -3%, a second stainless steel wire mesh matched with the shape of the mud discharging groove is covered above the mud discharging groove, and the mesh size of the second stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding cavity; mud discharge branch pipes are reserved in the wetland side walls corresponding to the mud discharge grooves, and the outer ends of the mud discharge branch pipes are connected with a mud discharge main pipe.\|[0008] Further, a water inlet has been seted up on one side of the above-mentioned inlet channel, be equipped with sludge settling tank at the mud main pipe output of arranging, the sludge settling tank top is equipped with the apron, sludge settling tank lateral part is equipped with the supernatant delivery port, supernatant delivery port and water inlet intercommunication, bottom intermediate position at sludge settling tank has been seted up and has been gathered mud groove, gather the inclined plane of sludge settling tank bottom for having certain slope on mud groove both sides, be close to the low side that is of gathering mud groove one side, be equipped with the slush pump in gathering mud groove, the slush pump is connected with power mud conveying pipe, the output of power mud conveying pipe extends to the sludge settling tank outside.\|[0009] Furthermore, a bracket is laid under the aeration main pipe and the branch pipe, and the end part of the bracket is fixedly connected with the bottom of the aeration reoxygenation chamber.\|[0010] Preferably, the immobilized microorganism is a DTG immobilized microorganism.\|[0011] Further, the thickness control of above-mentioned first compound filler, the compound filler of second, the compound filler of third and the compound filler of fourth is at 10 ~ 50mm, is equipped with the lower gravel layer that thickness is 60 ~ 100mm in the bottom of each layer compound filler, is equipped with the last gravel layer that thickness is 5 ~ 10mm at the top of each layer compound filler, is equipped with the three-layer nylon net at last gravel layer top, has laid the upper earthing at the three-layer nylon net top, is provided with the afforestation vegetation on the earthing of upper strata.\|[0012] Furthermore, the slope of the slope structures at the bottoms of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber is 2 percent.\|[0013] Furthermore, a sludge discharge valve is independently arranged on each sludge discharge branch pipe, and a main sludge discharge pipe is provided with a main valve.\|[0014] The artificial wetland process at least comprises the following beneficial effects:\|[0015] the constructed wetland system adopts an artificial construction mode to construct a pool body, which comprises an aeration reoxygenation chamber, an enhanced decarbonization chamber, an enhanced denitrification chamber, an enhanced dephosphorization chamber, a sludge sedimentation tank and the like. The water inlet channel mainly has the functions of uniformly distributing water and collecting purified water; the aeration reoxygenation chamber is a main body unit for purifying water quality, mainly comprising an aeration device, a composite filler and plants, and when polluted water flows through the unit module, the water quality can be purified by virtue of the composite filler, soil filtration, aquatic plants, efficient microorganism activities and the like; the composite filler can select different centralized fillers according to the quality of inlet water and the water quality target required to be achieved, so that the designed enhanced decarbonization chamber, enhanced denitrification chamber, enhanced dephosphorization chamber and sludge sedimentation tank can effectively remove nitrogen, phosphorus, heavy metals, impurity sludge and the like in the water body, and the accumulated impurity sludge or suspended matters are collected into the sedimentation tank through the inclination, sludge discharge pipes, sludge discharge grooves, sludge discharge branches/main pipes and the like arranged along the bottom of the tank body of each chamber and then discharged out through the slurry pump.\|DRAWINGS DESCRIPTION\|[0016] The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:\|[0017] fig. 1 is a plan layout view of an artificial wetland system of the present invention;\|[0018] FIG. 2 is a schematic diagram of the arrangement structure of a sludge discharge pipe at the bottom of the constructed wetland system of the invention;\|[0019] FIG. 3 is a cross-sectional view taken at A-A of FIG. 1;\|[0020] FIG. 4 is a cross-sectional view at B-B in FIG. 1 (intended to illustrate the structural level of the wetland from bottom to top);\|[0021] FIG. 5 is a cross-sectional view taken at C-C of FIG. 1;\|[0022] labeled as: 1. an aeration reoxygenation chamber; 2. an intensified decarbonization chamber; 3. a reinforced denitrification chamber; 4. strengthening a dephosphorization chamber; 5. a water inlet channel; 6. an observation room; 7. a drainage channel; 8. a water inlet; 9. a first overflow pipe; 10. a main pipe; 11. a support; 12. a first composite filler; 13. a second overflow tube; 14. a second composite filler; 15. a third overflow pipe; 16. a first reserved water pipe; 17. a third composite filler; 18. a fourth overflow pipe; 19. a fourth composite filler; 20. a second reserved water pipe; 21. a lower gravel layer; 22. an upper gravel layer; 23. three layers of nylon nets; 24. covering soil on the upper layer; 25. greening vegetation; 26. a sludge discharge pipe; 27. a sludge discharge groove; 28. a sludge discharge branch pipe; 29. a sludge discharge main pipe; 30. a mud valve; 31. a main valve; 32. a sludge sedimentation tank; 33. a cover plate; 34. a water outlet; 35. a sludge gathering tank; 36. a slurry pump; 37. a power mud conveying pipe; 38. and (4) isolating nets.\|INVENTION MODE\|Detailed Description\|[0023] In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention.\|[0024] Referring to fig. 1-3, the present invention provides a modular combined enhanced denitrification and dephosphorization artificial wetland process, i.e., a multi-stage novel subsurface flow artificial wetland system. Specifically, the system mainly comprises the following four processing units: an aeration reoxygenation chamber 1 (wetland purification area), an enhanced decarbonization chamber 2, an enhanced denitrification chamber 3 and an enhanced dephosphorization chamber 4, wherein a water inlet channel 5 (water collecting area) is arranged in front of the aeration reoxygenation chamber 1, an observation chamber 6 is arranged between the enhanced decarbonization chamber 2 and the enhanced denitrification chamber 3, and a water discharge channel 7 is arranged behind the enhanced dephosphorization chamber 4.\|[0025] Wherein, a water inlet 8 is arranged on one side of the water inlet channel 5, the water inlet channel 5 is communicated with the aeration reoxygenation chamber 1 through a first overflow pipe 9 arranged above, a main pipe 10 and a branch pipe (not shown) are arranged below the aeration reoxygenation chamber 1, the outer end of the main pipe 10 is connected with an aeration device (not shown), and the main pipe 10 and the branch pipe are arranged to play an aeration role in the water body of the aeration reoxygenation chamber 1. Furthermore, a support 11 is laid under the aeration main pipe 10 and the branch pipes, which mainly plays a role of supporting the aeration pipeline, and the end part of the support 11 is fixedly connected to the bottom of the aeration reoxygenation chamber 1.\|[0026] Referring to fig. 3 again, the aeration reoxygenation chamber 1 is filled with a first composite filler 12, and the first composite filler 12 is two or more of crushed stone with large particle size, gravel, volcanic rock and suspended ceramsite, wherein the suspended ceramsite contains immobilized microorganisms, and the immobilized microorganisms are preferably DTG immobilized microorganisms.\|[0027] In light of the above, the enhanced decarbonization chamber 2 is located behind the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2 is communicated with the aeration reoxygenation chamber 1 through a second overflow pipe 13 arranged above, and the enhanced decarbonization chamber 2 is filled with a second composite filler 14, wherein the second composite filler 14 mainly comprises gravel, broken stone and limestone.\|[0028] The enhanced denitrification chamber 3 is positioned behind the observation chamber 6, a third overflow pipe 15 and a first reserved water pipe 16 are respectively arranged on two sides of the observation chamber 6, the third overflow pipe 15 is communicated with the enhanced decarbonization chamber 2 and the observation chamber 6, and the first reserved water pipe 16 is arranged at the bottom and is communicated with the observation chamber 6 and the enhanced denitrification chamber 3; further, the reinforced denitrification chamber 3 is filled with a third composite filler 17, and the third composite filler 17 mainly comprises gravel, biochar and crushed stone.\|[0029] The enhanced dephosphorization chamber 4 is positioned behind the enhanced denitrification chamber 3, the enhanced dephosphorization chamber 4 is communicated with the enhanced denitrification chamber 3 through a fourth overflow pipe 18 arranged above, and a fourth composite filler 19 is filled in the enhanced dephosphorization chamber, wherein the fourth composite filler 19 mainly comprises gravel, zeolite, fly ash and broken stone. The enhanced phosphorus removal chamber 4 is communicated with the drainage channel 7 through a second reserved water pipe 20 arranged at the bottom.\|[0030] Referring to fig. 4, preferably, aquatic plants are planted above the first composite filler 12, the second composite filler 14, the third composite filler 17 and the fourth composite filler 19, so as to provide plant root adsorption for purifying the water in each chamber; preferably, the thicknesses of the first composite filler 12, the second composite filler 14, the third composite filler 17 and the fourth composite filler 19 are 10-50 mm, the bottom of each layer of composite filler is provided with a lower gravel layer 21 with the thickness of 60-100 mm, the top of each layer of composite filler is provided with an upper gravel layer 22 with the thickness of 5-10 mm, the top of the upper gravel layer 22 is provided with a three-layer nylon net 23, the top of the three-layer nylon net 23 is paved with upper-layer soil cover 24, and greening vegetation 25 (namely aquatic plants) is paved on the upper-layer soil cover 24.\|[0031] Referring to fig. 2 and 3 again, the bottoms of the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4 are slope structures with slopes of 2%, that is, the bottom of the water inlet side and the height of the water outlet side [ slope 2% ((height difference/horizontal distance between the water outlet side and the water inlet side) x 100%). Simultaneously at the pre-buried many mud pipes 26 that are provided with of above-mentioned each cavity bottom, furtherly, mud pipe 26 lays on the slope, and mud pipe 26 both ends have the slope equally, have seted up a plurality of holes side by side along the tube length direction at mud pipe 26 to be equipped with rather than shape assorted first stainless steel net (not shown) in drill way department, the mesh size of first stainless steel net should be less than the minimum particle diameter that corresponds compound filler in the cavity.\|[0032] In the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4 are all provided with the sludge discharge groove 27 at the lower side of the slope, the lower end of the sludge discharge pipe 26 is connected to the sludge discharge groove 27, the sludge discharge pipe 26 and the sludge discharge groove 27 are in a vertical connection state in the spatial position, the slope of the bottom of the long edge of the sludge discharge groove 27 is set to be 2% -3%, the sludge discharge groove 27 is covered with a second stainless steel wire net (not shown) matched with the shape of the sludge discharge pipe, and the mesh size of the second stainless steel wire net is smaller than the minimum particle size of the composite filler in the corresponding chamber. Mud discharging branch pipes 28 are reserved in the wetland side walls corresponding to the mud discharging grooves 27, the outer ends of the mud discharging branch pipes 28 are connected with a mud discharging main pipe 29, mud discharging valves 30 are independently arranged on the mud discharging branch pipes 28, and a main valve 31 is arranged on the mud discharging main pipe 29.\|[0033] Referring to fig. 5, a sludge settling tank 32 is disposed at an output end of the main sludge discharge pipe 29, a cover plate 33 is disposed at a top of the sludge settling tank 32, a supernatant outlet 34 is disposed at a side portion of the sludge settling tank 32, the supernatant outlet 34 is communicated with the water inlet 8 on the water inlet channel 5, a sludge collecting groove 35 is disposed at a middle position of a bottom of the sludge settling tank 32, the bottoms of the sludge settling tanks 32 on two sides of the sludge collecting groove 35 are inclined planes with a certain gradient (gradient is 2%), and a lower side is disposed at a side close to the sludge collecting groove 35, so that sludge can be automatically collected into the sludge collecting groove 35 under the action of gravity, a sludge pump 36 is fixedly disposed in the sludge collecting groove 35, the sludge pump 36 is connected with a power sludge conveying pipe 37, and the power sludge conveying pipe 37 penetrates through the sludge settling tank 32 and extends to the outside.\|[0034] After the constructed wetland system disclosed by the invention normally operates, the whole wetland system or a certain single module (namely four units of the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4) can be regularly controlled to carry out wetland sludge discharge operation through the sludge discharge valve 30 and the main valve 31, and water in the drainage channel 7 can be used for recharging back to carry out back flushing, so that the sludge discharge operation is carried out more efficiently, and the wetland blocking phenomenon is improved. The discharged sludge enters the sludge sedimentation tank 32 for sedimentation and can be discharged by a mud pump 36, and the supernatant liquid of the sludge sedimentation tank 32 flows back to the water inlet channel 5 through the water outlet 34.\|[0035] The invention can be suitable for all artificial wetland designs, such as tail water deep treatment of sewage plants, decentralized sewage treatment (such as rural sewage treatment) and the like; in practice, the pipe diameters and the numbers of the overflow pipes (the first overflow pipe 9, the second overflow pipe 13, the third overflow pipe 15, and the fourth overflow pipe 18) at the respective positions can be adjusted and changed according to actual needs, and a partition net 38 is provided above the inlet channel 5, the observation chamber 6, and the drain channel 7.\|[0036] Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.	(CN113683197)\|TECHNICAL FIELD\|[0001] The invention relates to the technical field of sewage treatment, in particular to an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system.\|BACKGROUND ART\|[0002] The artificial wetland is a technology for treating sewage and sludge by using the physical, chemical and biological triple synergistic action of soil, artificial medium, plants and microorganisms in the process of flowing along a certain direction by using sewage and sludge which are controllably dosed to the artificially constructed wetland from the artificially constructed and controlled-operation ground similar to the marshland. The action mechanism of the plant nutrient solution comprises the actions of adsorption, detention, filtration, oxidation reduction, precipitation, microbial decomposition, transformation, plant shielding, residue accumulation, transpiration moisture and nutrient absorption and various animals.\|[0003] However, the conventional subsurface flow constructed wetland has insufficient dissolved oxygen and the denitrification effect is difficult to meet the strict emission standard, so the current challenges are to effectively balance the oxygen demand and input in the artificial system under the condition of reducing the cost and how to design a system which can ensure the treatment efficiency and keep the system simple and economic in the aspects of layout, construction and maintenance. And because the suspended substances in the sewage are intercepted and the biological membranes on the surface of the substrate are accumulated and shed, the artificial wetland is easy to block in the actual operation.\|DISCLOSURE\|Disclosure of Invention\|[0004] Aiming at the problems in the prior art, the invention provides an artificial wetland ecological restoration process.\|[0005] In order to achieve the purpose, the invention is realized by the following technical scheme:\|[0006] an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system comprises an aeration reoxygenation chamber, a reinforced decarbonization chamber, a reinforced denitrification chamber and a reinforced phosphorus removal chamber, wherein a water inlet channel is arranged on the front side of the aeration reoxygenation chamber, an observation chamber is arranged between the reinforced decarbonization chamber and the reinforced denitrification chamber, and a water drainage channel is arranged on the rear side of the reinforced phosphorus removal chamber; the water inlet channel is communicated with the aeration reoxygenation chamber through a first overflow pipe, a main pipe and a branch pipe are arranged below the aeration reoxygenation chamber, and the outer end of the main pipe is connected with an aeration device; filling a first composite filler in the aeration reoxygenation chamber, wherein the first composite filler comprises at least two of large-particle-size crushed stone, gravel, volcanic rock and suspended ceramsite, and the suspended ceramsite contains immobilized microorganisms; the strengthening decarbonization chamber is positioned at the rear side of the aeration reoxygenation chamber and is communicated with the aeration reoxygenation chamber through a second overflow pipe, and second composite fillers are filled in the strengthening decarbonization chamber and comprise gravels, broken stones and limestone; the enhanced denitrification chamber is positioned at the rear side of the observation chamber, a third overflow pipe and a first reserved water pipe are respectively arranged at two sides of the observation chamber, the third overflow pipe is communicated with the enhanced decarbonization chamber and the observation chamber, and the first reserved water pipe is arranged at the bottom and is communicated with the observation chamber and the enhanced denitrification chamber; a third composite filler is filled in the enhanced denitrification chamber, and comprises gravels, charcoal and broken stones; the reinforced dephosphorization chamber is positioned at the rear side of the reinforced denitrification chamber, the reinforced dephosphorization chamber is communicated with the reinforced denitrification chamber through a fourth overflow pipe, a fourth composite filler is filled in the reinforced dephosphorization chamber, the fourth composite filler comprises gravel, zeolite, fly ash and broken stone, and the reinforced dephosphorization chamber is communicated with the drainage channel through a second reserved water pipe arranged at the bottom;\|[0007] the bottom of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber is of a slope structure, a plurality of sludge discharge pipes are pre-buried at the bottoms of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber and laid on the slope, a plurality of holes are arranged in the sludge discharge pipes side by side along the length direction of the pipes, a first stainless steel wire mesh matched with the shape of the first stainless steel wire mesh is arranged at an orifice, and the mesh size of the first stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding chamber; a mud discharging groove is formed in the lower side of the slope structure, the lower end of the mud discharging pipe is connected to the mud discharging groove, the gradient of the bottom of the long side of the mud discharging groove is set to be 2% -3%, a second stainless steel wire mesh matched with the shape of the mud discharging groove is covered above the mud discharging groove, and the mesh size of the second stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding cavity; mud discharge branch pipes are reserved in the wetland side walls corresponding to the mud discharge grooves, and the outer ends of the mud discharge branch pipes are connected with a mud discharge main pipe.\|[0008] Further, a water inlet has been seted up on one side of the above-mentioned inlet channel, be equipped with sludge settling tank at the mud main pipe output of arranging, the sludge settling tank top is equipped with the apron, sludge settling tank lateral part is equipped with the supernatant delivery port, supernatant delivery port and water inlet intercommunication, bottom intermediate position at sludge settling tank has been seted up and has been gathered mud groove, gather the inclined plane of sludge settling tank bottom for having certain slope on mud groove both sides, be close to the low side that is of gathering mud groove one side, be equipped with the slush pump in gathering mud groove, the slush pump is connected with power mud conveying pipe, the output of power mud conveying pipe extends to the sludge settling tank outside.\|[0009] Furthermore, a bracket is laid under the aeration main pipe and the branch pipe, and the end part of the bracket is fixedly connected with the bottom of the aeration reoxygenation chamber.\|[0010] Preferably, the immobilized microorganism is a DTG immobilized microorganism.\|[0011] Further, the thickness control of above-mentioned first compound filler, the compound filler of second, the compound filler of third and the compound filler of fourth is at 10 ~ 50mm, is equipped with the lower gravel layer that thickness is 60 ~ 100mm in the bottom of each layer compound filler, is equipped with the last gravel layer that thickness is 5 ~ 10mm at the top of each layer compound filler, is equipped with the three-layer nylon net at last gravel layer top, has laid the upper earthing at the three-layer nylon net top, is provided with the afforestation vegetation on the earthing of upper strata.\|[0012] Furthermore, the slope of the slope structures at the bottoms of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber is 2 percent.\|[0013] Furthermore, a sludge discharge valve is independently arranged on each sludge discharge branch pipe, and a main sludge discharge pipe is provided with a main valve.\|[0014] The artificial wetland process at least comprises the following beneficial effects:\|[0015] the constructed wetland system adopts an artificial construction mode to construct a pool body, which comprises an aeration reoxygenation chamber, an enhanced decarbonization chamber, an enhanced denitrification chamber, an enhanced dephosphorization chamber, a sludge sedimentation tank and the like. The water inlet channel mainly has the functions of uniformly distributing water and collecting purified water; the aeration reoxygenation chamber is a main body unit for purifying water quality, mainly comprising an aeration device, a composite filler and plants, and when polluted water flows through the unit module, the water quality can be purified by virtue of the composite filler, soil filtration, aquatic plants, efficient microorganism activities and the like; the composite filler can select different centralized fillers according to the quality of inlet water and the water quality target required to be achieved, so that the designed enhanced decarbonization chamber, enhanced denitrification chamber, enhanced dephosphorization chamber and sludge sedimentation tank can effectively remove nitrogen, phosphorus, heavy metals, impurity sludge and the like in the water body, and the accumulated impurity sludge or suspended matters are collected into the sedimentation tank through the inclination, sludge discharge pipes, sludge discharge grooves, sludge discharge branches/main pipes and the like arranged along the bottom of the tank body of each chamber and then discharged out through the slurry pump.\|DRAWINGS DESCRIPTION\|[0016] The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:\|[0017] fig. 1 is a plan layout view of an artificial wetland system of the present invention;\|[0018] FIG. 2 is a schematic diagram of the arrangement structure of a sludge discharge pipe at the bottom of the constructed wetland system of the invention;\|[0019] FIG. 3 is a cross-sectional view taken at A-A of FIG. 1;\|[0020] FIG. 4 is a cross-sectional view at B-B in FIG. 1 (intended to illustrate the structural level of the wetland from bottom to top);\|[0021] FIG. 5 is a cross-sectional view taken at C-C of FIG. 1;\|[0022] labeled as: 1. an aeration reoxygenation chamber; 2. an intensified decarbonization chamber; 3. a reinforced denitrification chamber; 4. strengthening a dephosphorization chamber; 5. a water inlet channel; 6. an observation room; 7. a drainage channel; 8. a water inlet; 9. a first overflow pipe; 10. a main pipe; 11. a support; 12. a first composite filler; 13. a second overflow tube; 14. a second composite filler; 15. a third overflow pipe; 16. a first reserved water pipe; 17. a third composite filler; 18. a fourth overflow pipe; 19. a fourth composite filler; 20. a second reserved water pipe; 21. a lower gravel layer; 22. an upper gravel layer; 23. three layers of nylon nets; 24. covering soil on the upper layer; 25. greening vegetation; 26. a sludge discharge pipe; 27. a sludge discharge groove; 28. a sludge discharge branch pipe; 29. a sludge discharge main pipe; 30. a mud valve; 31. a main valve; 32. a sludge sedimentation tank; 33. a cover plate; 34. a water outlet; 35. a sludge gathering tank; 36. a slurry pump; 37. a power mud conveying pipe; 38. and (4) isolating nets.\|INVENTION MODE\|Detailed Description\|[0023] In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention.\|[0024] Referring to fig. 1-3, the present invention provides a modular combined enhanced denitrification and dephosphorization artificial wetland process, i.e., a multi-stage novel subsurface flow artificial wetland system. Specifically, the system mainly comprises the following four processing units: an aeration reoxygenation chamber 1 (wetland purification area), an enhanced decarbonization chamber 2, an enhanced denitrification chamber 3 and an enhanced dephosphorization chamber 4, wherein a water inlet channel 5 (water collecting area) is arranged in front of the aeration reoxygenation chamber 1, an observation chamber 6 is arranged between the enhanced decarbonization chamber 2 and the enhanced denitrification chamber 3, and a water discharge channel 7 is arranged behind the enhanced dephosphorization chamber 4.\|[0025] Wherein, a water inlet 8 is arranged on one side of the water inlet channel 5, the water inlet channel 5 is communicated with the aeration reoxygenation chamber 1 through a first overflow pipe 9 arranged above, a main pipe 10 and a branch pipe (not shown) are arranged below the aeration reoxygenation chamber 1, the outer end of the main pipe 10 is connected with an aeration device (not shown), and the main pipe 10 and the branch pipe are arranged to play an aeration role in the water body of the aeration reoxygenation chamber 1. Furthermore, a support 11 is laid under the aeration main pipe 10 and the branch pipes, which mainly plays a role of supporting the aeration pipeline, and the end part of the support 11 is fixedly connected to the bottom of the aeration reoxygenation chamber 1.\|[0026] Referring to fig. 3 again, the aeration reoxygenation chamber 1 is filled with a first composite filler 12, and the first composite filler 12 is two or more of crushed stone with large particle size, gravel, volcanic rock and suspended ceramsite, wherein the suspended ceramsite contains immobilized microorganisms, and the immobilized microorganisms are preferably DTG immobilized microorganisms.\|[0027] In light of the above, the enhanced decarbonization chamber 2 is located behind the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2 is communicated with the aeration reoxygenation chamber 1 through a second overflow pipe 13 arranged above, and the enhanced decarbonization chamber 2 is filled with a second composite filler 14, wherein the second composite filler 14 mainly comprises gravel, broken stone and limestone.\|[0028] The enhanced denitrification chamber 3 is positioned behind the observation chamber 6, a third overflow pipe 15 and a first reserved water pipe 16 are respectively arranged on two sides of the observation chamber 6, the third overflow pipe 15 is communicated with the enhanced decarbonization chamber 2 and the observation chamber 6, and the first reserved water pipe 16 is arranged at the bottom and is communicated with the observation chamber 6 and the enhanced denitrification chamber 3; further, the reinforced denitrification chamber 3 is filled with a third composite filler 17, and the third composite filler 17 mainly comprises gravel, biochar and crushed stone.\|[0029] The enhanced dephosphorization chamber 4 is positioned behind the enhanced denitrification chamber 3, the enhanced dephosphorization chamber 4 is communicated with the enhanced denitrification chamber 3 through a fourth overflow pipe 18 arranged above, and a fourth composite filler 19 is filled in the enhanced dephosphorization chamber, wherein the fourth composite filler 19 mainly comprises gravel, zeolite, fly ash and broken stone. The enhanced phosphorus removal chamber 4 is communicated with the drainage channel 7 through a second reserved water pipe 20 arranged at the bottom.\|[0030] Referring to fig. 4, preferably, aquatic plants are planted above the first composite filler 12, the second composite filler 14, the third composite filler 17 and the fourth composite filler 19, so as to provide plant root adsorption for purifying the water in each chamber; preferably, the thicknesses of the first composite filler 12, the second composite filler 14, the third composite filler 17 and the fourth composite filler 19 are 10-50 mm, the bottom of each layer of composite filler is provided with a lower gravel layer 21 with the thickness of 60-100 mm, the top of each layer of composite filler is provided with an upper gravel layer 22 with the thickness of 5-10 mm, the top of the upper gravel layer 22 is provided with a three-layer nylon net 23, the top of the three-layer nylon net 23 is paved with upper-layer soil cover 24, and greening vegetation 25 (namely aquatic plants) is paved on the upper-layer soil cover 24.\|[0031] Referring to fig. 2 and 3 again, the bottoms of the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4 are slope structures with slopes of 2%, that is, the bottom of the water inlet side and the height of the water outlet side [ slope 2% ((height difference/horizontal distance between the water outlet side and the water inlet side) x 100%). Simultaneously at the pre-buried many mud pipes 26 that are provided with of above-mentioned each cavity bottom, furtherly, mud pipe 26 lays on the slope, and mud pipe 26 both ends have the slope equally, have seted up a plurality of holes side by side along the tube length direction at mud pipe 26 to be equipped with rather than shape assorted first stainless steel net (not shown) in drill way department, the mesh size of first stainless steel net should be less than the minimum particle diameter that corresponds compound filler in the cavity.\|[0032] In the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4 are all provided with the sludge discharge groove 27 at the lower side of the slope, the lower end of the sludge discharge pipe 26 is connected to the sludge discharge groove 27, the sludge discharge pipe 26 and the sludge discharge groove 27 are in a vertical connection state in the spatial position, the slope of the bottom of the long edge of the sludge discharge groove 27 is set to be 2% -3%, the sludge discharge groove 27 is covered with a second stainless steel wire net (not shown) matched with the shape of the sludge discharge pipe, and the mesh size of the second stainless steel wire net is smaller than the minimum particle size of the composite filler in the corresponding chamber. Mud discharging branch pipes 28 are reserved in the wetland side walls corresponding to the mud discharging grooves 27, the outer ends of the mud discharging branch pipes 28 are connected with a mud discharging main pipe 29, mud discharging valves 30 are independently arranged on the mud discharging branch pipes 28, and a main valve 31 is arranged on the mud discharging main pipe 29.\|[0033] Referring to fig. 5, a sludge settling tank 32 is disposed at an output end of the main sludge discharge pipe 29, a cover plate 33 is disposed at a top of the sludge settling tank 32, a supernatant outlet 34 is disposed at a side portion of the sludge settling tank 32, the supernatant outlet 34 is communicated with the water inlet 8 on the water inlet channel 5, a sludge collecting groove 35 is disposed at a middle position of a bottom of the sludge settling tank 32, the bottoms of the sludge settling tanks 32 on two sides of the sludge collecting groove 35 are inclined planes with a certain gradient (gradient is 2%), and a lower side is disposed at a side close to the sludge collecting groove 35, so that sludge can be automatically collected into the sludge collecting groove 35 under the action of gravity, a sludge pump 36 is fixedly disposed in the sludge collecting groove 35, the sludge pump 36 is connected with a power sludge conveying pipe 37, and the power sludge conveying pipe 37 penetrates through the sludge settling tank 32 and extends to the outside.\|[0034] After the constructed wetland system disclosed by the invention normally operates, the whole wetland system or a certain single module (namely four units of the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4) can be regularly controlled to carry out wetland sludge discharge operation through the sludge discharge valve 30 and the main valve 31, and water in the drainage channel 7 can be used for recharging back to carry out back flushing, so that the sludge discharge operation is carried out more efficiently, and the wetland blocking phenomenon is improved. The discharged sludge enters the sludge sedimentation tank 32 for sedimentation and can be discharged by a mud pump 36, and the supernatant liquid of the sludge sedimentation tank 32 flows back to the water inlet channel 5 through the water outlet 34.\|[0035] The invention can be suitable for all artificial wetland designs, such as tail water deep treatment of sewage plants, decentralized sewage treatment (such as rural sewage treatment) and the like; in practice, the pipe diameters and the numbers of the overflow pipes (the first overflow pipe 9, the second overflow pipe 13, the third overflow pipe 15, and the fourth overflow pipe 18) at the respective positions can be adjusted and changed according to actual needs, and a partition net 38 is provided above the inlet channel 5, the observation chamber 6, and the drain channel 7.\|[0036] Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.	Family Number\|(97182255)\|97182255\|Abstract\|(CN113683197 A)\|The invention discloses an efficient nitrogen and phosphorus removal anti - blocking constructed wetland system , and relates to the technical field of constructed wetland construction . The system comprises an aeration reoxygenation chamber , an enhanced carbon removal chamber , an enhanced nitrogen removal chamber , an enhanced phosphorus removal chamber , a sludge sedimentation tank and the like . A water inlet channel is mainly used for uniformly distributing water and collecting purified water . The aeration reoxygenation chamber is a main body unit for water quality purification and mainly comprises an aeration device , composite filler and plants , and when a polluted water body flows through the unit module , the water quality can be purified by virtue of the composite filler , soil filtration , and activities of aquatic plants , high - efficiency microorganisms and the like . According to the water quality of inlet water and the water quality target needing to be achieved , different concentrated and matched fillers can be selected , so that the enhanced carbon removal chamber , the enhanced nitrogen removal chamber , the enhanced phosphorus removal chamber and the sludge sedimentation tank which are designed and obtained can effectively remove nitrogen , phosphorus , heavy metal , impurity sludge and the like in the water body . \|Independent Claims\|(CN113683197 A)\|( . . . ) a first composite filler ( 12 ) is filled in the aeration reoxygenation chamber ( 1 ) , the first composite filler ( 12 ) comprises at least two of large - particle - size crushed stone , gravel , volcanic rock and suspended ceramsite , and the suspended ceramsite contains immobilized microorganisms ; ( . . . ) \|	Environmental technology	C02F-001/00/1\|C02F-001/52\|C02F-003/10\|C02F-003/10/7\|C02F-003/10/8\|C02F-003/32\|C02F-009/00\|C02F-2001/007\|C02F-2003/001\|C02F-2101/105\|C02F-2101/20\|C02F-2209/22		C02F-001/00/1\|C02F-001/52\|C02F-003/10\|C02F-003/10/7\|C02F-003/10/8\|C02F-003/32\|C02F-009/00\|C02F-2001/007\|C02F-2003/001\|C02F-2101/105\|C02F-2101/20\|C02F-2209/22	C02F-003/32\|C02F-009/14\|C02F-101/10\|C02F-101/20	C02F-003/32\|C02F-009/14\|C02F-101/10\|C02F-101/20			CN114804550B	CN114804550B 101123923 WHO=Examiner SELF=N	CN110294531\|CN107662979\|CN103819004\|CN103739081\|CN105967334\|KR100631373	CN110294531 86184402 WHO=Examiner SELF=N CAT=Y\|CN107662979 78700132 WHO=Examiner SELF=N CAT=Y\|CN103819004 66109297 WHO=Examiner SELF=N CAT=Y\|CN103739081 65358640 WHO=Examiner SELF=N CAT=Y\|CN105967334 74265238 WHO=Examiner SELF=N CAT=A\|KR100631373 33903977 WHO=Examiner SELF=N CAT=A		KR100631373; CN103739081; CN103819004; CN105967334; CN107662979; CN110294531		REVOKED	(CN113683197)\|REVOKED	DEAD	(CN113683197)\|DEAD	(CN113683197)\|LEGAL DETAILS FOR CN113683197\|Actual or expected expiration date=2023-06-23\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2021-08-16\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202110935649\|Application date=2021-08-16\|Standardized application number=2021CN-0935649\|Event publication date=2021-11-23\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN113683197\|Publication stage code=A\|Publication date=2021-11-23\|Standardized publication number=CN113683197\|Event publication date=2021-11-23\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2021-12-10\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2023-06-23\|Event code=CN/RJ01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Rejection of an application after its publication			https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQk2O2zXRvU8Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000059980367&ekey=2211&xpn=CN113683197&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=fcS77sZ%252Bq2lEYTuaxuvPxpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN113683197)\|CN	(CN113683197)\|NAME=ANHUI XINYU ECOLOGICAL IND CO LTD , COUNTRY=CN		(CN113683197)\|NAME=WANG XIAOJUN;Hefei Daozhi Intellectual Property Agency Co., Ltd. , REG=34130		(CN113683197)\|NAME=ZHANG YOUDE\|NAME=HE JIANJUN\|NAME=DAI CAOPEI\|NAME=ZHANG TIANTIAN	(CN113683197)\|5	1	1					(CN113683197)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2021-11-23\|Gazette number: GAZNUM=37-4801\|Number of Pages: NPAGES=9\|		(CN113683197)\|CHINESE (CHI)	(CN113683197)\|Patent	Titre: (CN113683197)\|Efficient nitrogen and phosphorus removal anti-blocking constructed wetland system Résumé: (CN113683197)\|The invention discloses an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system, and relates to the technical field of constructed wetland construction. The system comprises an aeration reoxygenation chamber, an enhanced carbon removal chamber, an enhanced nitrogen removal chamber, an enhanced phosphorus removal chamber, a sludge sedimentation tank and the like. A water inlet channel is mainly used for uniformly distributing water and collecting purified water. The aeration reoxygenation chamber is a main body unit for water quality purification and mainly comprises an aeration device, composite filler and plants, and when a polluted water body flows through the unit module, the water quality can be purified by virtue of the composite filler, soil filtration, and activities of aquatic plants, high-efficiency microorganisms and the like. According to the water quality of inlet water and the water quality target needing to be achieved, different concentrated and matched fillers can be selected, so that the enhanced carbon removal chamber, the enhanced nitrogen removal chamber, the enhanced phosphorus removal chamber and the sludge sedimentation tank which are designed and obtained can effectively remove nitrogen, phosphorus, heavy metal, impurity sludge and the like in the water body.	26	Abstract	gpt-4o-mini	no	The article focuses on a constructed wetland system for nitrogen and phosphorus removal, with no mention of enhanced weathering or CO₂ capture.
26	CN202311235173	CN202311235173	CN117404069	108167543	CN117404069 A 2024-01-16 [CN117404069]	2023-09-22	2023-09-22	2024-01-16		(CN117404069)\|2043-09-22	(CN117404069)\|Coiled tubing dragging type supercritical water injection coal rock underground gasification method	(CN117404069)\|The invention provides a coiled tubing dragging type supercritical water injection coal rock underground gasification method. The method comprises the following steps that 1, water with the temperature being 374.3 DEG C or above is injected into a coal seam through a draggable continuous oil pipe, the pressure in the continuous oil pipe and the pressure of the shaft bottom are controlled to be 22.1 MPa or above, high-temperature and high-speed supercritical water jet is sprayed out to crush coal rock, the supercritical water reacts with coal to obtain combustible gas, and meanwhile a gasification cavity is formed; 2, after the gasification cavity is formed, dragging the draggable coiled tubing to a next position, and repeating the jet flow process to form another gasification cavity; and 3, discharging the combustible gas out of the ground, and carrying out gas-water separation to recover H2. According to the technical scheme, the coal underground gasification technology can assist in efficient utilization of deep coal seam resources, can be organically coupled with a carbon dioxide capture, utilization and burying technology, and is expected to effectively absorb and digest CO2 generated in the coal combustion process.	CHINA UNIVERSITY OF PETROLEUM BEIJING	(CN117404069)\|CHINA UNIVERSITY OF PETROLEUM (BEIJING) ([CN])	YANG RUIYUE\|HUANG ZHONGWEI\|JING MEIYANG\|WU XIAOGUANG\|LI JINGBIN\|HONG CHUNYANG\|CHEN JIANXIANG\|QIN XIAOZHOU	(CN117404069)\|YANG RUIYUE\|HUANG ZHONGWEI\|JING MEIYANG\|WU XIAOGUANG\|LI JINGBIN\|HONG CHUNYANG\|CHEN JIANXIANG\|QIN XIAOZHOU	(CN117404069)\|YAO LIANG;BEIJING SANYOU INTELLECTUAL PROPERTY AGENCY LTD\|Reg. Nb: 11127\|HAN LEI;BEIJING SANYOU INTELLECTUAL PROPERTY AGENCY LTD\|Reg. Nb: 11127	(CN117404069)\|The cavitation gasification method has the advantages of increasing the contact area, improving the efficiency and the like.\|	(CN117404069)\|1. A continuous oil pipe dragging type supercritical water injection coal rock underground gasification method comprises the following steps:step 1: injecting water with the temperature of 374.3 ℃ or higher into a coal bed through a draggable continuous oil pipe, controlling the pressure in the continuous oil pipe and the pressure at the bottom of the well to be 22.1MPa or higher, injecting high-temperature and high-speed supercritical water jet to break up coal and rock, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;step 2: after forming the gasification cavity, dragging the draggable continuous oil pipe to the next position, and repeating the jet flow process to form another gasification cavity;step 3: discharging the combustible gas to the ground and recovering H by gas-water separation 2 。\|	(CN117404069)\|In order to solve the technical problems, the invention aims to provide the underground coal and rock gasification method which is based on the dragging type continuous oil pipe and supercritical water injection coal and rock technology and is beneficial to the efficient utilization of deep coal seam resources. In order to achieve the above purpose, the invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|The invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method.\|The invention relates to a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, and belongs to the technical field of coal gasification.\|	(CN117404069)\|UNDERGROUND GASIFICATION CAVITY(100,1)\|COAL COMBUSTIONCO(89,1)\|DRAG GABLE OIL PIPE(86,4)\|COMBUSTIBLE GAS(84,14)\|DEEP COAL SEAM RESOURCE(72,2)\|GASIFICATION CHAMBER(65,5)\|COAL BED(62,5)\|TARGET COAL SEAM(40,2)\|BYPRODUCT(38,1)\|UNDERGROUND COAL GASIFICATION(37,2)\|FIRING(36,1)\|COILED TUBING(34,7)\|ENTIRE COAL SEAM(31,1)\|SPRAY GUN TOOL(30,4)\|COAL UNDERGROUND GASIFICATION ENGINEERING(27,1)\|FORMATION CONDITION(27,1)\|ANNULUS(26,5)\|GASIFICATION CAVITY TRANSFORMATION(17,1)\|GAS WATER SEPARATION(16,7)\|CARBON DIOXIDE(16,2)\|POWER ASSISTED(15,2)\|SUPERCRITICAL WATER INJECTION COAL(14,3)\|DEEP COAL RESERVOIR(14,1)\|MULTIPOINT TRANSFORMATION(14,1)\|ORGANIC MATTER(14,1)\|SYNCHRONOUS REFORMING(14,1)\|HORIZONTAL WELL(12,6)\|CHINA UNIVERSITY(12,1)\|COAL COMBUSTION(12,1)\|COAL ROCK(12,1)\|COMBUSTION CONTINUITY(12,1)\|COMBUSTION EXPLOITATION(12,1)\|GASIFICATION FURNACE(12,1)\|HOMOGENEOUS OXIDIZATION(12,1)\|HYDRAULIC JETTING(12,1)\|UCG ENGINEERING(12,1)\|UNDERGROUND ACCURATE BUTT JOINT(12,1)\|HEAT PRESERVATION(10,2)\|PERMEABILITY(10,2)\|WATER VAPOR(10,2)\|COMBUSTION DYNAMIC(10,1)\|DYNAMIC COMBUSTION MONITORING(10,1)\|PHOSPHATING TREATMENT(10,1)\|REFORMED CAVITY(10,1)\|SHALLOW COAL SEAM(10,1)\|SMOOTH PROCEEDING(10,1)\|CN114607278B(9,2)\|BURYING(8,1)\|COMPRESSIBILITY(8,1)\|CONTROLLABLE GAS INJECTION(8,1)\|CRIP(8,1)\|GASIFIER CONSTRUCTION(8,1)\|GEOLOGICAL CONDITION(8,1)\|GROUND SEPARATION TANK(8,1)\|PRACTICABILITY(8,1)\|RESISTANT SPRAY GUN(8,1)\|STRATUM CONDITION(8,1)\|	(CN117404069)\|1. A continuous oil pipe dragging type supercritical water injection coal rock underground gasification method comprises the following steps:\|step 1: injecting water with the temperature of 374.3 ℃ or higher into a coal bed through a draggable continuous oil pipe, controlling the pressure in the continuous oil pipe and the pressure at the bottom of the well to be 22.1MPa or higher, injecting high-temperature and high-speed supercritical water jet to break up coal and rock, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|step 2: after forming the gasification cavity, dragging the draggable continuous oil pipe to the next position, and repeating the jet flow process to form another gasification cavity;\|step 3: discharging the combustible gas to the ground and recovering H by gas-water separation 2 。\|2. The method of claim 1, wherein the step of ejecting a high temperature, high velocity supercritical water jet to break up coal rock is accomplished by a lance tool;\|preferably, the lance tool is a cavitation lance in CN114607278B or CN 111395964B.\|3. The method of claim 1, wherein the reaction of supercritical water with coal comprises:\|coal + supercritical water → CO 2 +H 2 +CH 4 ;\|CO 2 +coal→co;\|organic matter +O 2 →CO 2 +H 2 O。\|4. A method according to claim 1 or 3, wherein the method further comprises capturing and/or separating CO at the surface 2 And injecting the coal bed into the gasification cavity.\|5. The method according to claim 1 or 4, wherein CO is captured and/or separated in the gasification chamber 2 Reacts with carbon in the coal bed at high temperature to generate CO, and the CO further reacts with water vapor to generate H 2 And CO 2 And obtaining the combustible gas.\|6. The method according to claim 1 or 4, wherein the main component of the combustible gas is CH 4 、H 2 、CO。\|7. The method according to claim 1 or 4, wherein the method comprises the steps of: CO obtained by separating gas from water 2 And injecting the mixture into a gasification cavity of the coal bed to participate in the reaction in the gasification cavity.\|8. The method of claim 1, wherein the method further comprises the steps of: and drilling the horizontal well into the coal seam, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m.\|9. The method of claim 1, wherein step 2 is repeated and the number of times the gasification chamber is formed is adjusted according to the actual formation conditions until the entire coal seam is fully utilized.\|10. The method according to any one of claims 1-9, comprising the specific steps of:\|(1) Drilling a horizontal well to a target coal seam, wherein the distances between the horizontal well and a top plate and a bottom plate of the coal seam are respectively more than or equal to 1m;\|(2) A continuous oil pipe provided with a spray gun tool is put into a coal bed;\|(3) Injecting high-temperature water with the temperature of more than 374.3 ℃ into the coiled tubing from the ground;\|(4) Controlling the pressure in the coiled tubing and the pressure at the bottom of the well to be more than 22.1MPa, spraying high-temperature and high-speed supercritical water jet at the bottom of the well to break coal and rock at the bottom of the well, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|(5) After forming the gasification cavity, dragging the continuous oil pipe to the next position, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|(6) The combustible gas is discharged out of the ground through an annulus, and H is recovered after gas-water separation on the ground 2 ;\|(7) Separating the ground from the obtained CO 2 The byproducts are re-injected into the underground gasification cavity to participate in the reaction in the gasification cavity.	(CN117404069)\|TECHNICAL FIELD\|[0001] The invention relates to a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, and belongs to the technical field of coal gasification.\|BACKGROUND ART\|[0002] Underground coal gasification technology (UCG) is controlled combustion of underground coal in situ to produce CH 4 、H 2 The process of combustible gas such as CO and the like is a coal clean development and utilization technology integrating three processes of well construction, coal mining and gasification, can promote the development and utilization of deep coal seams, greatly improves the resource utilization efficiency, is used as a potential coal clean exploitation means, is not applied in a large scale due to the restriction of factors such as technology and economy, and still is in an engineering test stage and needs to be subjected to key technology attack. In addition, the existing engineering test projects mainly adopt shallow coal seams, and the technology is relatively mature.\|[0003] However, compared with the shallow coal seam, the underground gasification of the deep coal is more advantageous in the aspect of environmental protection, but the deep coal seam has the characteristics of high ground stress, medium and high temperature, extremely low permeability, high saturation, strong compressibility and the like, and the key technology for restricting the development of the underground gasification of the deep coal is further required to be overcome.\|[0004] In recent years, the key engineering technology of the UCG (deep coal reservoir) mainly surrounds the U-shaped gasifier construction technology and the controllable gas injection point back-off gasification process (CRIP). However, because underground coal gasification is in-situ combustion exploitation of coal, in order to keep combustion continuity, the drilling rate of a coal bed in a horizontal well section is theoretically required to reach 100%, and the well track control of the horizontal well and the underground accurate butt joint of the horizontal well and a production vertical well bring great challenges to the construction of a U-shaped gasification furnace. The CRIP technology is applicable to the feasibility of deep coal underground gasification engineering, but the coal seam is shallower in the current field test, and the applicability is still to be further practically checked.\|DISCLOSURE\|Disclosure of Invention\|[0005] In order to solve the technical problems, the invention aims to provide the underground coal and rock gasification method which is based on the dragging type continuous oil pipe and supercritical water injection coal and rock technology and is beneficial to the efficient utilization of deep coal seam resources.\|[0006] In order to achieve the above purpose, the invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|[0007] step 1: injecting water with the temperature of 374.3 ℃ or higher into a coal bed through a draggable continuous oil pipe, controlling the pressure in the continuous oil pipe and the pressure at the bottom of the well to be 22.1MPa or higher, injecting high-temperature and high-speed supercritical water jet to break up coal and rock, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|[0008] step 2: after forming the gasification cavity, dragging the draggable continuous oil pipe to the next position, and repeating the jet flow process to form another gasification cavity;\|[0009] step 3: discharging the combustible gas to the ground and recovering H by gas-water separation 2 。\|[0010] According to a specific embodiment of the present invention, preferably, the high temperature water is heated at the surface to a temperature of not less than 374.3 ℃ and then injected into the coal seam through the coiled tubing.\|[0011] According to the specific embodiment of the invention, preferably, the high-temperature water is injected by adopting an oil pipe, and the annular space is in a closed state in the process, so that the heat preservation effect is realized while the bottom hole pressure is controlled.\|[0012] According to the specific embodiment of the invention, the pressure in the oil pipe and the bottom hole pressure are preferably controlled to be more than 22.1MPa, so that the injected high temperature water can be in a supercritical state at 374.3 ℃.\|[0013] According to a specific embodiment of the present invention, preferably, the step of ejecting the supercritical water jet at high temperature and high speed to break up coal and rock is implemented by a spray gun tool.\|[0014] According to a specific embodiment of the present invention, preferably, the spray gun tool is a hole-making spray gun in CN114607278B or CN111395964B, which has good temperature and pressure resistance.\|[0015] According to the specific embodiment of the invention, the high-temperature high-speed supercritical water jet flow is adopted to efficiently break the coal and rock, so that the subsequent reaction is quickened, the gasification cavity transformation effect is improved, the construction time is shortened, and the construction cost is saved. Meanwhile, jet flow can generate stress disturbance to form a pressure relief area, so that pressure relief, reflection increase and income improvement are realized, and cost reduction and efficiency increase are achieved.\|[0016] According to the specific embodiment of the invention, the supercritical water forms supercritical water jet flow through the spray gun tool, so that the supercritical water continuously reacts with coal to convert coal chemical energy into hydrogen energy due to the characteristics of high temperature and high pressure, homogeneous oxidation and the like of the supercritical water while efficiently breaking coal and rock. Preferably, the reaction of supercritical water with coal comprises:\|[0017] coal + supercritical water → CO 2 +H 2 +CH 4 ;\|[0018] CO 2 +coal→co;\|[0019] organic matter +O 2 →CO 2 +H 2 O。\|[0020] According to a particular embodiment of the invention, the CO is preferably to be captured and/or separated at the surface 2 And injecting the coal bed into the gasification cavity.\|[0021] According to a particular embodiment of the invention, the CO is preferably captured and/or separated in the gasification chamber 2 Reacts with carbon in the coal seam at high temperature to produce CO, which further reacts with water vapor (formed from supercritical water) to produce H 2 And CO 2 And obtaining the combustible gas.\|[0022] According to a specific embodiment of the present invention, preferably, the main component of the combustible gas is CH 4 、H 2 CO, etc.\|[0023] According to a specific embodiment of the present invention, preferably, the combustible gas formed in the gasification chamber is exhausted to the ground through the annulus, and the produced fluid is subjected to gas-water separation in the ground separation tank, and clean fuel H is separated and recovered 2 。\|[0024] According to a specific embodiment of the invention, preferably, the method comprises the steps of: will beCO obtained by gas-water separation 2 And injecting the mixture into a gasification cavity of the coal bed to participate in the reaction in the gasification cavity. Through the reciprocating circulation process, the method is expected to effectively absorb and digest CO generated in the coal combustion process 2 。\|[0025] According to a specific embodiment of the present invention, preferably, the method further comprises the steps of: and drilling the horizontal well into the coal seam, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m.\|[0026] According to a specific embodiment of the present invention, the step 2 is preferably repeated, and the number of times of forming the gasification chamber is repeated is adjusted according to the actual stratum condition until the whole coal seam is fully utilized.\|[0027] According to a particular embodiment of the invention, the method preferably comprises the following specific steps:\|[0028] (1) Drilling a horizontal well to a target coal seam, wherein the distances between the horizontal well and a top plate and a bottom plate of the coal seam are respectively more than or equal to 1m;\|[0029] (2) A continuous oil pipe provided with a spray gun tool is put into a coal bed;\|[0030] (3) Injecting high-temperature water with the temperature of more than 374.3 ℃ into the coiled tubing from the ground;\|[0031] (4) Controlling the pressure in the coiled tubing and the pressure at the bottom of the well to be more than 22.1MPa, spraying high-temperature and high-speed supercritical water jet at the bottom of the well to break coal and rock at the bottom of the well, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|[0032] (5) After smoothly reforming the gasification cavity, dragging the continuous oil pipe to the next position, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|[0033] (6) The combustible gas is discharged out of the ground through an annulus, and H is recovered after gas-water separation on the ground 2 ;\|[0034] (7) Separating the ground from the obtained CO 2 The byproducts are re-injected into the underground gasification cavity to participate in the reaction in the gasification cavity.\|[0035] The continuous oil pipe dragging type supercritical water injection coal rock underground gasification method provided by the invention is suitable for deep coal seam resources, such as deep coal seams with the burial depth of 1500-3000 m.\|[0036] The technical scheme of the invention is that the Underground Coal Gasification (UCG) technology can be used for capturing and utilizing carbon dioxide and is organically coupled with the burying technology (UCG-CCUS) while the power-assisted deep coal seam resources are utilized efficiently, and is expected to effectively absorb and digest CO generated in the coal combustion process 2 。\|[0037] The method provided by the invention breaks the coal and rock by means of supercritical water jet impact, and breaks the coal and rock to improve the construction efficiency and gasification efficiency while forming a better reaction cavity, and can react in the gasification cavity, so that the gasification can be easier to carry out by breaking the coal blocks, the effect is better, and the jet can generate stress disturbance to form a pressure relief area, so that the pressure relief and permeability improvement can be realized. The cavitation gasification method has the advantages of increasing the contact area, improving the efficiency and the like. In addition, the method provided by the invention can realize multi-point transformation through one well and one pipe column, does not need ignition of a combustion well, has simple process, strong practicability and low cost, and can be used for transformation of a deep coal seam.\|[0038] The invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method by combining the advantages of a CRIP process, a continuous oil pipe technology and a supercritical water jet technology. The method of the invention can not only convey gasifying agent and igniter to the bottom of the well in UCG engineering, but also bind with temperature, pressure and other sensors to realize the combustion dynamic monitoring function, thereby controlling the injection of gasifying agent according to geological conditions and coal bed characteristics to ensure that the whole combustion process is stable and the produced components are optimal.\|DRAWINGS DESCRIPTION\|[0039] Fig. 1 is a schematic diagram of a coal underground gasification method of coiled tubing dragging type supercritical water injection coal rock according to embodiment 1 of the present invention.\|INVENTION MODE\|Detailed Description\|[0040] The technical solution of the present invention will be described in detail below for a clearer understanding of technical features, objects and advantageous effects of the present invention, but should not be construed as limiting the scope of the present invention.\|[0041] Example 1\|[0042] The embodiment provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|[0043] (1) Drilling a horizontal well to a gasification reforming target coal seam with a burial depth of 1500-3000m, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m, so that the whole process is smoothly carried out in the target coal seam;\|[0044] (2) The continuous oil pipe is utilized to send a spray gun tool to a preset reconstruction point, the spray gun tool uses a high-pressure resistant, temperature resistant and wear resistant spray gun (a hole-making spray gun in CN114607278B, CN 111395964B) developed by China university of Petroleum (Beijing), the bearing temperature is-30 ℃ to 100 ℃, the working pressure bearing pressure is 70MPa at maximum, the surface is subjected to phosphating treatment, the corrosion resistance is enhanced, the spraying speed can reach 250m/s, and the coal rock can be efficiently impacted and broken;\|[0045] (3) Injecting high-temperature water with the temperature of more than or equal to 374.3 ℃ into the coiled tubing from the ground, injecting the high-temperature water into the tubing, wherein an annulus is in a closed state in the process, controlling the bottom hole pressure and simultaneously playing a role in heat preservation;\|[0046] (4) The pressure in the continuous oil pipe and the pressure at the bottom of the well are controlled at 22.1MPa, high-temperature and high-speed supercritical water jet is sprayed at the bottom of the well, the characteristics of high temperature and high pressure, homogeneous oxidization and the like of supercritical water are utilized to continuously react with coal while the coal is crushed, a large amount of heat is released in the reaction process, the smooth proceeding of the subsequent reaction is maintained, the coal chemical energy is converted into hydrogen energy in the whole process, the combustible gas is obtained, and a gasification cavity is formed;\|[0047] (5) After the gasification cavity is formed, the synchronous reforming effect of pressure relief and permeability increase can be achieved on the coal bed around the reformed cavity during reaction, and the gas yield is increased. After a first gasification cavity is smoothly transformed, dragging the continuous oil pipe to the next position, transforming the point spacing to 20m, determining a plurality of transformation points by adopting a geometric dividing method, dragging a spray gun by using the continuous oil pipe, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|[0048] (6) Discharging the combustible gas (gas-water mixture) from the ground through the annulus, and recovering H after gas-water separation on the ground 2 ;\|[0049] (7) Separating the ground from the obtained CO 2 Gasification chamber with byproduct reinjection into the groundThe gasification chamber is used for trapping and utilizing again.\|[0050] Fig. 1 is a schematic diagram of a coal underground gasification method of coiled tubing dragging type supercritical water injection coal rock according to embodiment 1 of the present invention. The dragging type continuous oil pipe can realize fixed-point, directional and multiple hydraulic jetting, can be combined with monitoring technologies such as temperature, pressure and the like to realize dynamic combustion monitoring, and reasonably selects the cavity-building times according to site construction conditions, construction requirements, reservoir conditions and the like.	(CN117404069)\|TECHNICAL FIELD\|[0001] The invention relates to a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, and belongs to the technical field of coal gasification.\|BACKGROUND ART\|[0002] Underground coal gasification technology (UCG) is controlled combustion of underground coal in situ to produce CH 4 、H 2 The process of combustible gas such as CO and the like is a coal clean development and utilization technology integrating three processes of well construction, coal mining and gasification, can promote the development and utilization of deep coal seams, greatly improves the resource utilization efficiency, is used as a potential coal clean exploitation means, is not applied in a large scale due to the restriction of factors such as technology and economy, and still is in an engineering test stage and needs to be subjected to key technology attack. In addition, the existing engineering test projects mainly adopt shallow coal seams, and the technology is relatively mature.\|[0003] However, compared with the shallow coal seam, the underground gasification of the deep coal is more advantageous in the aspect of environmental protection, but the deep coal seam has the characteristics of high ground stress, medium and high temperature, extremely low permeability, high saturation, strong compressibility and the like, and the key technology for restricting the development of the underground gasification of the deep coal is further required to be overcome.\|[0004] In recent years, the key engineering technology of the UCG (deep coal reservoir) mainly surrounds the U-shaped gasifier construction technology and the controllable gas injection point back-off gasification process (CRIP). However, because underground coal gasification is in-situ combustion exploitation of coal, in order to keep combustion continuity, the drilling rate of a coal bed in a horizontal well section is theoretically required to reach 100%, and the well track control of the horizontal well and the underground accurate butt joint of the horizontal well and a production vertical well bring great challenges to the construction of a U-shaped gasification furnace. The CRIP technology is applicable to the feasibility of deep coal underground gasification engineering, but the coal seam is shallower in the current field test, and the applicability is still to be further practically checked.\|DISCLOSURE\|Disclosure of Invention\|[0005] In order to solve the technical problems, the invention aims to provide the underground coal and rock gasification method which is based on the dragging type continuous oil pipe and supercritical water injection coal and rock technology and is beneficial to the efficient utilization of deep coal seam resources.\|[0006] In order to achieve the above purpose, the invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|[0007] step 1: injecting water with the temperature of 374.3 ℃ or higher into a coal bed through a draggable continuous oil pipe, controlling the pressure in the continuous oil pipe and the pressure at the bottom of the well to be 22.1MPa or higher, injecting high-temperature and high-speed supercritical water jet to break up coal and rock, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|[0008] step 2: after forming the gasification cavity, dragging the draggable continuous oil pipe to the next position, and repeating the jet flow process to form another gasification cavity;\|[0009] step 3: discharging the combustible gas to the ground and recovering H by gas-water separation 2 。\|[0010] According to a specific embodiment of the present invention, preferably, the high temperature water is heated at the surface to a temperature of not less than 374.3 ℃ and then injected into the coal seam through the coiled tubing.\|[0011] According to the specific embodiment of the invention, preferably, the high-temperature water is injected by adopting an oil pipe, and the annular space is in a closed state in the process, so that the heat preservation effect is realized while the bottom hole pressure is controlled.\|[0012] According to the specific embodiment of the invention, the pressure in the oil pipe and the bottom hole pressure are preferably controlled to be more than 22.1MPa, so that the injected high temperature water can be in a supercritical state at 374.3 ℃.\|[0013] According to a specific embodiment of the present invention, preferably, the step of ejecting the supercritical water jet at high temperature and high speed to break up coal and rock is implemented by a spray gun tool.\|[0014] According to a specific embodiment of the present invention, preferably, the spray gun tool is a hole-making spray gun in CN114607278B or CN111395964B, which has good temperature and pressure resistance.\|[0015] According to the specific embodiment of the invention, the high-temperature high-speed supercritical water jet flow is adopted to efficiently break the coal and rock, so that the subsequent reaction is quickened, the gasification cavity transformation effect is improved, the construction time is shortened, and the construction cost is saved. Meanwhile, jet flow can generate stress disturbance to form a pressure relief area, so that pressure relief, reflection increase and income improvement are realized, and cost reduction and efficiency increase are achieved.\|[0016] According to the specific embodiment of the invention, the supercritical water forms supercritical water jet flow through the spray gun tool, so that the supercritical water continuously reacts with coal to convert coal chemical energy into hydrogen energy due to the characteristics of high temperature and high pressure, homogeneous oxidation and the like of the supercritical water while efficiently breaking coal and rock. Preferably, the reaction of supercritical water with coal comprises:\|[0017] coal + supercritical water → CO 2 +H 2 +CH 4 ;\|[0018] CO 2 +coal→co;\|[0019] organic matter +O 2 →CO 2 +H 2 O。\|[0020] According to a particular embodiment of the invention, the CO is preferably to be captured and/or separated at the surface 2 And injecting the coal bed into the gasification cavity.\|[0021] According to a particular embodiment of the invention, the CO is preferably captured and/or separated in the gasification chamber 2 Reacts with carbon in the coal seam at high temperature to produce CO, which further reacts with water vapor (formed from supercritical water) to produce H 2 And CO 2 And obtaining the combustible gas.\|[0022] According to a specific embodiment of the present invention, preferably, the main component of the combustible gas is CH 4 、H 2 CO, etc.\|[0023] According to a specific embodiment of the present invention, preferably, the combustible gas formed in the gasification chamber is exhausted to the ground through the annulus, and the produced fluid is subjected to gas-water separation in the ground separation tank, and clean fuel H is separated and recovered 2 。\|[0024] According to a specific embodiment of the invention, preferably, the method comprises the steps of: will beCO obtained by gas-water separation 2 And injecting the mixture into a gasification cavity of the coal bed to participate in the reaction in the gasification cavity. Through the reciprocating circulation process, the method is expected to effectively absorb and digest CO generated in the coal combustion process 2 。\|[0025] According to a specific embodiment of the present invention, preferably, the method further comprises the steps of: and drilling the horizontal well into the coal seam, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m.\|[0026] According to a specific embodiment of the present invention, the step 2 is preferably repeated, and the number of times of forming the gasification chamber is repeated is adjusted according to the actual stratum condition until the whole coal seam is fully utilized.\|[0027] According to a particular embodiment of the invention, the method preferably comprises the following specific steps:\|[0028] (1) Drilling a horizontal well to a target coal seam, wherein the distances between the horizontal well and a top plate and a bottom plate of the coal seam are respectively more than or equal to 1m;\|[0029] (2) A continuous oil pipe provided with a spray gun tool is put into a coal bed;\|[0030] (3) Injecting high-temperature water with the temperature of more than 374.3 ℃ into the coiled tubing from the ground;\|[0031] (4) Controlling the pressure in the coiled tubing and the pressure at the bottom of the well to be more than 22.1MPa, spraying high-temperature and high-speed supercritical water jet at the bottom of the well to break coal and rock at the bottom of the well, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|[0032] (5) After smoothly reforming the gasification cavity, dragging the continuous oil pipe to the next position, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|[0033] (6) The combustible gas is discharged out of the ground through an annulus, and H is recovered after gas-water separation on the ground 2 ;\|[0034] (7) Separating the ground from the obtained CO 2 The byproducts are re-injected into the underground gasification cavity to participate in the reaction in the gasification cavity.\|[0035] The continuous oil pipe dragging type supercritical water injection coal rock underground gasification method provided by the invention is suitable for deep coal seam resources, such as deep coal seams with the burial depth of 1500-3000 m.\|[0036] The technical scheme of the invention is that the Underground Coal Gasification (UCG) technology can be used for capturing and utilizing carbon dioxide and is organically coupled with the burying technology (UCG-CCUS) while the power-assisted deep coal seam resources are utilized efficiently, and is expected to effectively absorb and digest CO generated in the coal combustion process 2 。\|[0037] The method provided by the invention breaks the coal and rock by means of supercritical water jet impact, and breaks the coal and rock to improve the construction efficiency and gasification efficiency while forming a better reaction cavity, and can react in the gasification cavity, so that the gasification can be easier to carry out by breaking the coal blocks, the effect is better, and the jet can generate stress disturbance to form a pressure relief area, so that the pressure relief and permeability improvement can be realized. The cavitation gasification method has the advantages of increasing the contact area, improving the efficiency and the like. In addition, the method provided by the invention can realize multi-point transformation through one well and one pipe column, does not need ignition of a combustion well, has simple process, strong practicability and low cost, and can be used for transformation of a deep coal seam.\|[0038] The invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method by combining the advantages of a CRIP process, a continuous oil pipe technology and a supercritical water jet technology. The method of the invention can not only convey gasifying agent and igniter to the bottom of the well in UCG engineering, but also bind with temperature, pressure and other sensors to realize the combustion dynamic monitoring function, thereby controlling the injection of gasifying agent according to geological conditions and coal bed characteristics to ensure that the whole combustion process is stable and the produced components are optimal.\|DRAWINGS DESCRIPTION\|[0039] Fig. 1 is a schematic diagram of a coal underground gasification method of coiled tubing dragging type supercritical water injection coal rock according to embodiment 1 of the present invention.\|INVENTION MODE\|Detailed Description\|[0040] The technical solution of the present invention will be described in detail below for a clearer understanding of technical features, objects and advantageous effects of the present invention, but should not be construed as limiting the scope of the present invention.\|[0041] Example 1\|[0042] The embodiment provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|[0043] (1) Drilling a horizontal well to a gasification reforming target coal seam with a burial depth of 1500-3000m, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m, so that the whole process is smoothly carried out in the target coal seam;\|[0044] (2) The continuous oil pipe is utilized to send a spray gun tool to a preset reconstruction point, the spray gun tool uses a high-pressure resistant, temperature resistant and wear resistant spray gun (a hole-making spray gun in CN114607278B, CN 111395964B) developed by China university of Petroleum (Beijing), the bearing temperature is-30 ℃ to 100 ℃, the working pressure bearing pressure is 70MPa at maximum, the surface is subjected to phosphating treatment, the corrosion resistance is enhanced, the spraying speed can reach 250m/s, and the coal rock can be efficiently impacted and broken;\|[0045] (3) Injecting high-temperature water with the temperature of more than or equal to 374.3 ℃ into the coiled tubing from the ground, injecting the high-temperature water into the tubing, wherein an annulus is in a closed state in the process, controlling the bottom hole pressure and simultaneously playing a role in heat preservation;\|[0046] (4) The pressure in the continuous oil pipe and the pressure at the bottom of the well are controlled at 22.1MPa, high-temperature and high-speed supercritical water jet is sprayed at the bottom of the well, the characteristics of high temperature and high pressure, homogeneous oxidization and the like of supercritical water are utilized to continuously react with coal while the coal is crushed, a large amount of heat is released in the reaction process, the smooth proceeding of the subsequent reaction is maintained, the coal chemical energy is converted into hydrogen energy in the whole process, the combustible gas is obtained, and a gasification cavity is formed;\|[0047] (5) After the gasification cavity is formed, the synchronous reforming effect of pressure relief and permeability increase can be achieved on the coal bed around the reformed cavity during reaction, and the gas yield is increased. After a first gasification cavity is smoothly transformed, dragging the continuous oil pipe to the next position, transforming the point spacing to 20m, determining a plurality of transformation points by adopting a geometric dividing method, dragging a spray gun by using the continuous oil pipe, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|[0048] (6) Discharging the combustible gas (gas-water mixture) from the ground through the annulus, and recovering H after gas-water separation on the ground 2 ;\|[0049] (7) Separating the ground from the obtained CO 2 Gasification chamber with byproduct reinjection into the groundThe gasification chamber is used for trapping and utilizing again.\|[0050] Fig. 1 is a schematic diagram of a coal underground gasification method of coiled tubing dragging type supercritical water injection coal rock according to embodiment 1 of the present invention. The dragging type continuous oil pipe can realize fixed-point, directional and multiple hydraulic jetting, can be combined with monitoring technologies such as temperature, pressure and the like to realize dynamic combustion monitoring, and reasonably selects the cavity-building times according to site construction conditions, construction requirements, reservoir conditions and the like.	Family Number\|(108167543)\|108167543\|Abstract\|(CN117404069 A)\|The invention provides a coiled tubing dragging type supercritical water injection coal rock underground gasification method . The method comprises the following steps that 1, water with the temperature being 374.3 DEG C or above is injected into a coal seam through a draggable continuous oil pipe , the pressure in the continuous oil pipe and the pressure of the shaft bottom are controlled to be 22.1 MPa or above , high - temperature and high - speed supercritical water jet is sprayed out to crush coal rock , the supercritical water reacts with coal to obtain combustible gas , and meanwhile a gasification cavity is formed ; 2, after the gasification cavity is formed , dragging the draggable coiled tubing to a next position , and repeating the jet flow process to form another gasification cavity ; and 3, discharging the combustible gas out of the ground , and carrying out gas - water separation to recover H2 . According to the technical scheme , the coal underground gasification technology can assist in efficient utilization of deep coal seam resources , can be organically coupled with a carbon dioxide capture , utilization and burying technology , and is expected to effectively absorb and digest CO2 generated in the coal combustion process . \|	Civil engineering	E21B-043/295\|E21B-047/00		E21B-043/295\|E21B-047/00	E21B-043/295\|E21B-047/00	E21B-043/295\|E21B-047/00			CN117823112B	CN117823112B 109209909 WHO=Examiner SELF=N	CN116575900\|CN114607278\|CN114607278B\|CN111395964\|CN110552678\|CN115853488\|CN101113670\|US20100288555	CN116575900 106093745 WHO=Examiner SELF=N CAT=Y\|CN114607278 100436537 WHO=Examiner SELF=Y CAT=Y\|CN114607278B 100436537 WHO=Examiner SELF=Y CAT=Y\|CN111395964 89650997 WHO=Examiner SELF=Y CAT=Y\|CN110552678 86927074 WHO=Examiner SELF=N CAT=Y\|CN115853488 104311160 WHO=Examiner SELF=N CAT=A\|CN101113670 6492399 WHO=Examiner SELF=N CAT=A\|US20100288555 14121274 WHO=Examiner SELF=N CAT=A		CN101113670; US20100288555; CN110552678; CN111395964; CN114607278; CN115853488; CN114607278B; CN116575900		PENDING	(CN117404069)\|PENDING	ALIVE	(CN117404069)\|ALIVE	(CN117404069)\|LEGAL DETAILS FOR CN117404069\|Actual or expected expiration date=2043-09-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-09-22\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202311235173\|Application date=2023-09-22\|Standardized application number=2023CN-1235173\|Event publication date=2024-01-16\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN117404069\|Publication stage code=A\|Publication date=2024-01-16\|Standardized publication number=CN117404069\|Event publication date=2024-01-16\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2024-02-02\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN117404069)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRcmltkk1GC9Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000071091443&ekey=1977&xpn=CN117404069&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=maHWLlLw9yeEcraFRbWWSZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN117404069)\|CN	(CN117404069)\|NAME=CHINA UNIVERSITY OF PETROLEUM (BEIJING) , COUNTRY=CN		(CN117404069)\|NAME=YAO LIANG;BEIJING SANYOU INTELLECTUAL PROPERTY AGENCY LTD , REG=11127NAME=HAN LEI;BEIJING SANYOU INTELLECTUAL PROPERTY AGENCY LTD , REG=11127		(CN117404069)\|NAME=YANG RUIYUE\|NAME=HUANG ZHONGWEI\|NAME=JING MEIYANG\|NAME=WU XIAOGUANG\|NAME=LI JINGBIN\|NAME=HONG CHUNYANG\|NAME=CHEN JIANXIANG\|NAME=QIN XIAOZHOU	(CN117404069)\|1	1	1					(CN117404069)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2024-01-16\|Gazette number: GAZNUM=40-0301\|Number of Pages: NPAGES=7\|		(CN117404069)\|CHINESE (CHI)	(CN117404069)\|Patent	Titre: (CN117404069)\|Coiled tubing dragging type supercritical water injection coal rock underground gasification method Résumé: (CN117404069)\|The invention provides a coiled tubing dragging type supercritical water injection coal rock underground gasification method. The method comprises the following steps that 1, water with the temperature being 374.3 DEG C or above is injected into a coal seam through a draggable continuous oil pipe, the pressure in the continuous oil pipe and the pressure of the shaft bottom are controlled to be 22.1 MPa or above, high-temperature and high-speed supercritical water jet is sprayed out to crush coal rock, the supercritical water reacts with coal to obtain combustible gas, and meanwhile a gasification cavity is formed; 2, after the gasification cavity is formed, dragging the draggable coiled tubing to a next position, and repeating the jet flow process to form another gasification cavity; and 3, discharging the combustible gas out of the ground, and carrying out gas-water separation to recover H2. According to the technical scheme, the coal underground gasification technology can assist in efficient utilization of deep coal seam resources, can be organically coupled with a carbon dioxide capture, utilization and burying technology, and is expected to effectively absorb and digest CO2 generated in the coal combustion process.	25	Abstract	gpt-4o-mini	no	The article focuses on underground gasification of coal and CO2 capture related to combustion, not on accelerated weathering or mineral carbonation processes.
27	CN202410256237	CN202410256237	CN117918078	109552031	CN117918078 A 2024-04-26 [CN117918078]	2024-03-06	2024-03-06	2024-04-26		(CN117918078)\|2044-03-06	(CN117918078)\|Method for improving soil and increasing carbon sink	(CN117918078)\|The invention discloses a method capable of improving soil and increasing carbon sink, and relates to the technical field of soil improvement, the method comprises a crusher and a dolomite raw material, the mined dolomite raw material is put into the crusher to obtain a small-size blocky dolomite raw material, the small-size blocky dolomite raw material is put into a preset grinding machine, and the grinding machine is used for grinding the small-size blocky dolomite raw material; the method comprises the following steps: crushing ground calcium carbonate to obtain powdery ground calcium carbonate, further containing the powdery ground calcium carbonate in an automatic scattering barrel, carrying the automatic scattering barrel through a preset unmanned aerial vehicle, and further uniformly scattering the powdery ground calcium carbonate into an external pretreatment ecological system; calcium carbonate in the ground calcium carbonate is attached to land and is subjected to a weathering reaction with rock, carbon dioxide in air is captured, an associated reaction is generated, and divalent calcium and bicarbonate radicals are obtained through the reaction. The soil conditioner can reduce acidity of soil, is beneficial to soil remediation, increases nutrient elements of the soil, and enhances the soil improvement effect.	INSTITUTE OF GEOCHEMISTRY - CHINESE ACADEMY OF SCIENCES	(CN117918078)\|INSTITUTE OF GEOCHEMISTRY CHINESE ACADEMY OF SCIENCES ([CN])	SHI LIANGXING\|CENG SIBO\|LIU ZAIHUA	(CN117918078)\|SHI LIANGXING\|CENG SIBO\|LIU ZAIHUA	(CN117918078)\|ZHANG XIAODONG;Beijing Blue Spider Patent Agency Co., Ltd.\|Reg. Nb: 16226	(CN117918078)\|1. the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application.\|The method has the advantages that the acidity of soil can be reduced by increasing the photosynthesis of the aquatic organisms absorbed by clean CO 2, the soil is beneficial to the restoration of the soil, the nutrient elements of the soil are increased, and the soil improvement effect is enhanced.\|The working principle is as follows: the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application.\|The above reasons lead to the fact that the existing soil is high in acidity, the soil is difficult to repair, the soil is poor in quality and lacks of nutrient substances, and the utilization rate of the soil is low.\|	(CN117918078)\|1. The method for improving soil and increasing carbon sink comprises a crusher and dolomite raw materials, and is characterized in that the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic scattering bucket, the automatic scattering bucket is carried by a preset unmanned plane, and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment; The calcium carbonate in the heavy calcium carbonate is attached to land, and is subjected to weathering reaction with rock to capture carbon dioxide in the air, and an accompanying reaction is generated to obtain divalent calcium and bicarbonate, so that calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment.\|	(CN117918078)\|The invention discloses a method capable of realizing soil improvement and increasing carbon sequestration, which relates to the technical field of soil improvement and comprises a crusher and dolomite raw materials, wherein the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic sprinkling barrel, the automatic sprinkling barrel is carried by a preset unmanned aerial vehicle, and the powdery heavy calcium carbonate is further uniformly sprinkled into an external pretreatment ecological system; the calcium carbonate in the heavy calcium carbonate is attached to land, and undergoes weathering reaction with rock to capture carbon dioxide in the air, and accompanying reaction is generated, so that divalent calcium and bicarbonate are obtained through the reaction.\|The invention relates to the technical field of soil improvement, in particular to a method capable of achieving soil improvement and increasing carbon sink.\|	(CN117918078)\|GROUND(100,16)\|CARBON SINK(100,13)\|SOIL IMPROVEMENT(100,9)\|AUTOMATIC SPRINKLING BARREL(99,2)\|POWDERY HEAVY CALCIUM CARBONATE(91,11)\|HEAVY POWDER(86,12)\|SOIL RESTORATION(64,2)\|PRESET GRINDER(58,4)\|CALCIUM CARBONATE(54,38)\|DIVALENT CALCIUM(49,4)\|PRESET UNMANNED PLANE(48,1)\|CRUSHER(47,7)\|CALCIUM CARBONATE CAPTURE(41,2)\|NUTRIENT SUBSTANCE(38,1)\|HEAVY CALCIUM CARBONATE(36,10)\|BICARBONATE(34,7)\|PRETREATMENT(34,5)\|MAGNESIUM ION(32,9)\|DIC FERTILIZATION(32,6)\|SMALL VOLUME BLOCKY DOLOMITE(31,8)\|SOIL AGGLOMERATE(31,1)\|RELIEVING ACIDIFICATION(28,5)\|PRESET UNMANNED AERIAL VEHICLE(28,3)\|CARBON SEQUESTRATION(27,3)\|RESTORATION TREATMENT(27,3)\|MINED DOLOMITE RAW MATERIAL(26,4)\|DOLOMITE RAW MATERIAL(25,7)\|BUCKET(22,6)\|PHOTOSYNTHESIS(22,2)\|WATER ALKALIZATION(21,1)\|ACIDITY(20,1)\|SMALL VOLUME BLOCKY(19,8)\|ROCK(19,3)\|CARBON DIOXIDE(17,16)\|BICARBONATE ION(17,3)\|DISSOLUTION REACTION(17,3)\|CARBONATE ION REACTION(17,2)\|PRETREATMENT ECOLOGICAL SYSTEM(17,2)\|EFFECTING SOIL IMPROVEMENT(17,1)\|AQUATIC ECOSYSTEM(16,6)\|LAND ECOLOGICAL SYSTEM(16,3)\|UNMANNED AERIAL VEHICLE(16,3)\|AQUATIC ORGANISM(15,5)\|RAW MATERIAL(14,15)\|ECOLOGICAL SYSTEM(14,10)\|REACTION PRODUCT(13,3)\|SOIL FERTILITY(12,4)\|CALCIUM ION(11,8)\|GREENHOUSE EFFECT(11,3)\|SOIL AGGREGATE(10,3)\|CACO(10,2)\|LARGE AREA POPULARIZATION(9,2)\|LOW COST BENEFIT(9,2)\|UTILIZATION RATE(9,1)\|LIGHT ACTION(8,1)\|CHEMICAL EQUATION(7,6)\|CO2(7,3)\|SOIL SUSTAINABILITY(7,1)\|DISSOLVED INORGANIC CARBON(6,12)\|ENDOGENOUS ORGANIC CARBON AOC(6,3)\|H2O MG(6,2)\|ABSORB NUTRIENT(6,1)\|SOIL ENVIRONMENT ECOLOGY(6,1)\|ABSORB AQUATIC ORGANISM(5,1)\|ABSORPTION AQUATIC ORGANISM(4,1)\|MOISTURE MANAGEMENT(4,1)\|WATER BODY ALKALIZATION(3,4)\|	(CN117918078)\|1. The method for improving soil and increasing carbon sink comprises a crusher and dolomite raw materials, and is characterized in that the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic scattering bucket, the automatic scattering bucket is carried by a preset unmanned plane, and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment;\| The calcium carbonate in the heavy calcium carbonate is attached to land, and is subjected to weathering reaction with rock to capture carbon dioxide in the air, and an accompanying reaction is generated to obtain divalent calcium and bicarbonate, so that calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. \|2. The method of claim 1, wherein the accompanying reaction comprises chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, and reacting the carbonate ions with carbon dioxide and water in the presence of sufficient carbon dioxide to produce bicarbonate ions.\|3. The method for improving soil and increasing carbon sequestration according to claim 2, wherein the chemical equation of the chemical dissolution reaction of heavy calcium carbonate with water is: mgCO 3+CaCO3+H2O—Mg2++Ca2++2CO32-.\|4. The method for improving soil and increasing carbon dioxide according to claim 2, wherein the chemical equation of the reaction of carbonate ions and carbon dioxide is CO 32-+CO2+H2O—2HCO3-.\|5. A method of effecting soil improvement and carbon sequestration according to claim 3 wherein said calcium and magnesium ions enter the soil system to form soil agglomerates which alter soil fertility.\|6. The method of claim 1, wherein the calcium carbonate is weathered to produce dissolved inorganic carbon, the dissolved inorganic carbon enters the aquatic ecosystem, the water is absorbed by adding clean CO 2, and light action occurs, so that the DIC fertilization effect is utilized to form an endogenous organic carbon AOC, and further, the organic carbon capable of relieving acidification or alkalization of the water is formed and stored in the water.	(CN117918078)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of soil improvement, in particular to a method capable of achieving soil improvement and increasing carbon sink.\|BACKGROUND ART\|[0002] Soil improvement refers to improving the texture, structure, fertility and moisture retention of soil through a series of measures and methods to increase the agricultural productivity and sustainability of the soil. The soil improvement method comprises the following steps: organic matter addition, mineral addition, pH adjustment, and moisture management.\|[0003] Carbon sink refers to a natural or artificial system capable of absorbing and storing isothermal chamber gases of carbon dioxide (CO 2). They can help reduce the greenhouse gas content in the atmosphere and mitigate global climate change. Natural carbon sinks include forest, wetland, grassland, ocean and other ecosystems. An artificial carbon sink is an artificially created system for absorbing and storing carbon dioxide.\|[0004] In the process of production activities, on one hand, human beings easily interfere with the soil surface layer and vegetation in the peripheral area of the production activities, so that the soil structure function is destroyed, the carbon sink capacity of the soil is reduced, and effective soil aggregates can not be formed to prevent loss of nutrients, thereby reducing the soil fertility and causing land degradation; on the other hand, in the soil which is partially engaged in production activities, such as mines, the large content of heavy metals can damage the capability of plants to absorb other nutrient elements, influence the microbial activity in the soil, and reduce the number of plants and microorganisms.\|[0005] The above reasons lead to the fact that the existing soil is high in acidity, the soil is difficult to repair, the soil is poor in quality and lacks of nutrient substances, and the utilization rate of the soil is low.\|[0006] The above information disclosed in this background section is only for enhancement of understanding of the background section of the invention and therefore it may not form the prior art that is already known to those of ordinary skill in the art.\|DISCLOSURE\|Disclosure of Invention\|[0007] Aiming at the technical problems existing in the existing soil ecological environment, the invention provides a method for improving soil and increasing carbon sink.\|[0008] The method for improving soil and increasing carbon sink comprises the steps of putting the mined dolomite raw materials into a crusher to obtain small-volume blocky dolomite raw materials, putting the small-volume blocky dolomite raw materials into a preset grinder to obtain powdery heavy calcium carbonate, further placing the powdery heavy calcium carbonate into an automatic scattering bucket, and carrying the automatic scattering bucket through a preset unmanned aerial vehicle to uniformly scatter the powdery heavy calcium carbonate into an external pretreatment ecological system;\|[0009] The calcium carbonate in the heavy calcium carbonate is attached to land, and is subjected to weathering reaction with rock to capture carbon dioxide in the air, and an accompanying reaction is generated to obtain divalent calcium and bicarbonate, so that calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. \|[0010] Further, the accompanying reaction comprises chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, and the carbonate ions react with carbon dioxide and water to generate bicarbonate ions in an environment with enough carbon dioxide.\|[0011] Further, the chemical equation of the chemical dissolution reaction of the heavy calcium carbonate and water is as follows: caMgCO 3+H2O+CO2—Mg2++Ca2++2HCO32-.\|[0012] Further, the chemical equation of the reaction of the carbonate ions and the carbon dioxide is CO 32-+CO2+H2O—2HCO3-.\|[0013] Further, the calcium ions and magnesium ions enter the soil system to form soil aggregates which can change the soil fertility.\|[0014] Furthermore, the calcium carbonate is weathered to generate dissolved inorganic carbon, the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed by adding clean CO 2, a light effect is generated, and further an endogenous organic carbon AOC is formed by using a DIC fertilization effect, so that organic carbon capable of relieving acidification or alkalization of a water body is formed and stored in the water body.\|[0015] The foregoing summary is for the purpose of the specification only and is not intended to be limiting in any way. In addition to the illustrative aspects, embodiments, and features described above, further aspects, embodiments, and features of the present invention will become apparent by reference to the drawings and the following detailed description.\|[0016] The invention has the beneficial effects that:\|[0017] 1. the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application. \|[0018] 2. The dissolved inorganic carbon is generated through calcium carbonate weathering, so that the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed through adding clean CO 2, the light effect is generated, and further, an endogenous organic carbon AOC is formed by using a DIC fertilization effect, and further, the organic carbon capable of relieving acidification or alkalization of a water body is formed to be stored in the water body, so that acidification of the water body can be relieved conveniently.\|DRAWINGS DESCRIPTION\|[0019] FIG. 1 is a schematic illustration of the reaction scheme of the present invention;\|[0020] Fig. 2 is a schematic diagram of the workflow of the present invention. \|INVENTION MODE\|Detailed Description\|[0021] It is noted that the figures are schematic and not drawn to scale. Relative dimensions and proportions of parts of the figures have been shown exaggerated or reduced in size, for the sake of clarity and convenience in the drawings, and any dimensions are merely illustrative and not limiting. The same reference numerals are used for the same structures, elements, or accessories appearing in more than two figures to embody similar features.\|[0022] Examples\|[0023] A method for improving soil and increasing carbon sink comprises a crusher and dolomite raw materials, wherein the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic scattering bucket, the automatic scattering bucket is carried by a preset unmanned aerial vehicle, and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment, such as a mine and an acidified water body.\|[0024] The calcium carbonate in heavy calcium carbonate is attached to land, and undergoes weathering reaction with rock to capture carbon dioxide in air, and accompanying reaction is generated, so that divalent calcium and bicarbonate are obtained through the reaction, and then calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. The calcium carbonate is ground into powder and is scattered into a land ecological system, so that the calcium carbonate can capture atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere can be reduced conveniently, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved.\|[0025] The accompanying reaction comprises the chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, wherein the chemical equation of the chemical dissolution reaction of the heavy calcium carbonate and water is as follows: mgCO 3+CaCO3+H2O—Mg2++Ca2++2CO32-. Calcium ions and magnesium ions enter the soil system to form soil aggregates which can change the soil fertility. The method has the advantages that the acidity of soil can be reduced by increasing the photosynthesis of the aquatic organisms absorbed by clean CO 2, the soil is beneficial to the restoration of the soil, the nutrient elements of the soil are increased, and the soil improvement effect is enhanced.\|[0026] And in the presence of sufficient carbon dioxide, the carbonate ions react with carbon dioxide and water to form bicarbonate ions. The chemical equation for the reaction of carbonate ions with carbon dioxide is CO 32-+CO2+H2O—2HCO3-. The calcium carbonate is weathered to generate dissolved inorganic carbon, the dissolved inorganic carbon enters into an aquatic ecosystem, the clean CO 2 is added to absorb aquatic organisms, the light effect is generated, and then the DIC fertilization effect is utilized to form endogenous organic carbon AOC, so that organic carbon capable of relieving acidification or alkalization of the water body is formed and stored in the water body. The dissolved inorganic carbon is generated through calcium carbonate weathering, so that the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed through adding clean CO 2, the light effect is generated, and further, an endogenous organic carbon AOC is formed by using a DIC fertilization effect, and further, the organic carbon capable of relieving acidification or alkalization of a water body is formed to be stored in the water body, so that acidification of the water body can be relieved conveniently.\|[0027] The working principle is as follows: the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application.\|[0028] And then through the calcium carbonate efflorescence production dissolved inorganic carbon, make dissolved inorganic carbon enter into aquatic ecosystem, through increasing clean CO 2 absorption aquatic organism, take place the photosynthesis, and then utilize DIC fertilization effect to form endogenous organic carbon AOC, and then form can alleviate the organic carbon of water acidizing or alkalization and preserve to the water in, be convenient for can alleviate the acidizing of water.\|[0029] In the description of the present invention, the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. The meaning of "a plurality of" is two or more, unless specifically defined otherwise.\|[0030] In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0031] In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.\|[0032] In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily for the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.\|[0033] In the drawings of the disclosed embodiments, only the structures related to the embodiments of the present disclosure are referred to, and other structures may refer to the general design, so that the same embodiment and different embodiments of the present disclosure may be combined with each other without conflict.\|[0034] Although the present invention has been described with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described, or equivalents may be substituted for elements thereof, and any modifications, equivalents, improvements and changes may be made without departing from the spirit and principles of the present invention.	(CN117918078)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of soil improvement, in particular to a method capable of achieving soil improvement and increasing carbon sink.\|BACKGROUND ART\|[0002] Soil improvement refers to improving the texture, structure, fertility and moisture retention of soil through a series of measures and methods to increase the agricultural productivity and sustainability of the soil. The soil improvement method comprises the following steps: organic matter addition, mineral addition, pH adjustment, and moisture management.\|[0003] Carbon sink refers to a natural or artificial system capable of absorbing and storing isothermal chamber gases of carbon dioxide (CO 2). They can help reduce the greenhouse gas content in the atmosphere and mitigate global climate change. Natural carbon sinks include forest, wetland, grassland, ocean and other ecosystems. An artificial carbon sink is an artificially created system for absorbing and storing carbon dioxide.\|[0004] In the process of production activities, on one hand, human beings easily interfere with the soil surface layer and vegetation in the peripheral area of the production activities, so that the soil structure function is destroyed, the carbon sink capacity of the soil is reduced, and effective soil aggregates can not be formed to prevent loss of nutrients, thereby reducing the soil fertility and causing land degradation; on the other hand, in the soil which is partially engaged in production activities, such as mines, the large content of heavy metals can damage the capability of plants to absorb other nutrient elements, influence the microbial activity in the soil, and reduce the number of plants and microorganisms.\|[0005] The above reasons lead to the fact that the existing soil is high in acidity, the soil is difficult to repair, the soil is poor in quality and lacks of nutrient substances, and the utilization rate of the soil is low.\|[0006] The above information disclosed in this background section is only for enhancement of understanding of the background section of the invention and therefore it may not form the prior art that is already known to those of ordinary skill in the art.\|DISCLOSURE\|Disclosure of Invention\|[0007] Aiming at the technical problems existing in the existing soil ecological environment, the invention provides a method for improving soil and increasing carbon sink.\|[0008] The method for improving soil and increasing carbon sink comprises the steps of putting the mined dolomite raw materials into a crusher to obtain small-volume blocky dolomite raw materials, putting the small-volume blocky dolomite raw materials into a preset grinder to obtain powdery heavy calcium carbonate, further placing the powdery heavy calcium carbonate into an automatic scattering bucket, and carrying the automatic scattering bucket through a preset unmanned aerial vehicle to uniformly scatter the powdery heavy calcium carbonate into an external pretreatment ecological system;\|[0009] The calcium carbonate in the heavy calcium carbonate is attached to land, and is subjected to weathering reaction with rock to capture carbon dioxide in the air, and an accompanying reaction is generated to obtain divalent calcium and bicarbonate, so that calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. \|[0010] Further, the accompanying reaction comprises chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, and the carbonate ions react with carbon dioxide and water to generate bicarbonate ions in an environment with enough carbon dioxide.\|[0011] Further, the chemical equation of the chemical dissolution reaction of the heavy calcium carbonate and water is as follows: caMgCO 3+H2O+CO2—Mg2++Ca2++2HCO32-.\|[0012] Further, the chemical equation of the reaction of the carbonate ions and the carbon dioxide is CO 32-+CO2+H2O—2HCO3-.\|[0013] Further, the calcium ions and magnesium ions enter the soil system to form soil aggregates which can change the soil fertility.\|[0014] Furthermore, the calcium carbonate is weathered to generate dissolved inorganic carbon, the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed by adding clean CO 2, a light effect is generated, and further an endogenous organic carbon AOC is formed by using a DIC fertilization effect, so that organic carbon capable of relieving acidification or alkalization of a water body is formed and stored in the water body.\|[0015] The foregoing summary is for the purpose of the specification only and is not intended to be limiting in any way. In addition to the illustrative aspects, embodiments, and features described above, further aspects, embodiments, and features of the present invention will become apparent by reference to the drawings and the following detailed description.\|[0016] The invention has the beneficial effects that:\|[0017] 1. the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application. \|[0018] 2. The dissolved inorganic carbon is generated through calcium carbonate weathering, so that the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed through adding clean CO 2, the light effect is generated, and further, an endogenous organic carbon AOC is formed by using a DIC fertilization effect, and further, the organic carbon capable of relieving acidification or alkalization of a water body is formed to be stored in the water body, so that acidification of the water body can be relieved conveniently.\|DRAWINGS DESCRIPTION\|[0019] FIG. 1 is a schematic illustration of the reaction scheme of the present invention;\|[0020] Fig. 2 is a schematic diagram of the workflow of the present invention. \|INVENTION MODE\|Detailed Description\|[0021] It is noted that the figures are schematic and not drawn to scale. Relative dimensions and proportions of parts of the figures have been shown exaggerated or reduced in size, for the sake of clarity and convenience in the drawings, and any dimensions are merely illustrative and not limiting. The same reference numerals are used for the same structures, elements, or accessories appearing in more than two figures to embody similar features.\|[0022] Examples\|[0023] A method for improving soil and increasing carbon sink comprises a crusher and dolomite raw materials, wherein the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic scattering bucket, the automatic scattering bucket is carried by a preset unmanned aerial vehicle, and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment, such as a mine and an acidified water body.\|[0024] The calcium carbonate in heavy calcium carbonate is attached to land, and undergoes weathering reaction with rock to capture carbon dioxide in air, and accompanying reaction is generated, so that divalent calcium and bicarbonate are obtained through the reaction, and then calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. The calcium carbonate is ground into powder and is scattered into a land ecological system, so that the calcium carbonate can capture atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere can be reduced conveniently, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved.\|[0025] The accompanying reaction comprises the chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, wherein the chemical equation of the chemical dissolution reaction of the heavy calcium carbonate and water is as follows: mgCO 3+CaCO3+H2O—Mg2++Ca2++2CO32-. Calcium ions and magnesium ions enter the soil system to form soil aggregates which can change the soil fertility. The method has the advantages that the acidity of soil can be reduced by increasing the photosynthesis of the aquatic organisms absorbed by clean CO 2, the soil is beneficial to the restoration of the soil, the nutrient elements of the soil are increased, and the soil improvement effect is enhanced.\|[0026] And in the presence of sufficient carbon dioxide, the carbonate ions react with carbon dioxide and water to form bicarbonate ions. The chemical equation for the reaction of carbonate ions with carbon dioxide is CO 32-+CO2+H2O—2HCO3-. The calcium carbonate is weathered to generate dissolved inorganic carbon, the dissolved inorganic carbon enters into an aquatic ecosystem, the clean CO 2 is added to absorb aquatic organisms, the light effect is generated, and then the DIC fertilization effect is utilized to form endogenous organic carbon AOC, so that organic carbon capable of relieving acidification or alkalization of the water body is formed and stored in the water body. The dissolved inorganic carbon is generated through calcium carbonate weathering, so that the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed through adding clean CO 2, the light effect is generated, and further, an endogenous organic carbon AOC is formed by using a DIC fertilization effect, and further, the organic carbon capable of relieving acidification or alkalization of a water body is formed to be stored in the water body, so that acidification of the water body can be relieved conveniently.\|[0027] The working principle is as follows: the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application.\|[0028] And then through the calcium carbonate efflorescence production dissolved inorganic carbon, make dissolved inorganic carbon enter into aquatic ecosystem, through increasing clean CO 2 absorption aquatic organism, take place the photosynthesis, and then utilize DIC fertilization effect to form endogenous organic carbon AOC, and then form can alleviate the organic carbon of water acidizing or alkalization and preserve to the water in, be convenient for can alleviate the acidizing of water.\|[0029] In the description of the present invention, the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. The meaning of "a plurality of" is two or more, unless specifically defined otherwise.\|[0030] In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0031] In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.\|[0032] In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily for the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.\|[0033] In the drawings of the disclosed embodiments, only the structures related to the embodiments of the present disclosure are referred to, and other structures may refer to the general design, so that the same embodiment and different embodiments of the present disclosure may be combined with each other without conflict.\|[0034] Although the present invention has been described with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described, or equivalents may be substituted for elements thereof, and any modifications, equivalents, improvements and changes may be made without departing from the spirit and principles of the present invention.	Family Number\|(109552031)\|109552031\|Object of Invention\|(CN117918078 A)\|The invention discloses a method capable of realizing soil improvement and increasing carbon sequestration , which relates to the technical field of soil improvement and comprises a crusher and dolomite raw materials , wherein the ( . . . ) pretreatment ecological system ; the calcium carbonate in the heavy calcium carbonate is attached to land , and undergoes weathering reaction with rock to capture carbon dioxide in the air , and accompanying reaction is generated , so that divalent calcium and bicarbonate are obtained through the reaction . \|Abstract\|(CN117918078 A)\|The invention discloses a method capable of improving soil and increasing carbon sink , and relates to the technical field of soil improvement , the method comprises a crusher and a dolomite raw material , the mined dolomite raw material is put into the crusher to obtain a small - size blocky dolomite raw material , the small - size blocky dolomite raw material is put into a preset grinding machine , and the grinding machine is used for grinding the small - size blocky dolomite raw material ; the method comprises the following steps : crushing ground calcium carbonate to obtain powdery ground calcium carbonate , further containing the powdery ground calcium carbonate in an automatic scattering barrel , carrying the automatic scattering barrel through a preset unmanned aerial vehicle , and further uniformly scattering the powdery ground calcium carbonate into an external pretreatment ecological system ; calcium carbonate in the ground calcium carbonate is attached to land and is subjected to a weathering reaction with rock , carbon dioxide in air is captured , an associated reaction is generated , and divalent calcium and bicarbonate radicals are obtained through the reaction . The soil conditioner can reduce acidity of soil , is beneficial to soil remediation , increases nutrient elements of the soil , and enhances the soil improvement effect . \|Advantages / Prev. Drawbacks\|(CN117918078 A)\|1. the calcium carbonate is ground into powder and scattered into a land ecological system , so that the calcium carbonate captures the atmospheric CO 2 through rock weathering , the content of CO 2 in the atmosphere is reduced , a certain effect of increasing carbon sink is achieved , and the greenhouse effect caused by CO 2 is further relieved ; the method has the advantages of simple operation , simple flow , low cost ( . . . ) \|The working principle is as follows : the calcium carbonate is ground into powder and scattered into a land ecological system , so that the calcium carbonate captures the atmospheric CO 2 through rock weathering , the content of CO 2 in the atmosphere is reduced , a certain effect of increasing carbon sink is achieved , and the greenhouse effect caused by CO 2 is further relieved ; the method has the advantages of simple operation , simple flow , low cost ( . . . ) \|Independent Claims\|(CN117918078 A)\|( . . . ) unmanned plane , and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment ; The calcium carbonate in the heavy calcium carbonate is attached to land , and is subjected to weathering reaction with rock to capture carbon dioxide in the air , and an accompanying reaction is generated to obtain divalent calcium and bicarbonate , so that calcium ions , magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment ( . . . ) \|	Other special machines	A01B-077/00\|A01B-079/00		A01B-077/00\|A01B-079/00	A01B-077/00\|A01B-079/00	A01B-077/00\|A01B-079/00					CN117101374\|CN106190157\|CN105295930	CN117101374 107464098 WHO=Examiner SELF=N CAT=A\|CN106190157 74809241 WHO=Examiner SELF=N CAT=A\|CN105295930 72139248 WHO=Examiner SELF=N CAT=A	李长江等: "《园林绿化与养护》", 31 January 2024, 中国电力出版社, pages: 213 - 214 (Cat. Y)\|安艳玲: "《贵州清水江流域生态环境保护与可持续管理》", 31 July 2017, 中国环境出版社, pages: 38 - 39 (Cat. Y)	CN105295930; CN106190157; CN117101374		PENDING	(CN117918078)\|PENDING	ALIVE	(CN117918078)\|ALIVE	(CN117918078)\|LEGAL DETAILS FOR CN117918078\|Actual or expected expiration date=2044-03-06\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-06\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202410256237\|Application date=2024-03-06\|Standardized application number=2024CN-0256237\|Event publication date=2024-04-26\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN117918078\|Publication stage code=A\|Publication date=2024-04-26\|Standardized publication number=CN117918078\|Event publication date=2024-04-26\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2024-05-14\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN117918078)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTaLIaZYZJUQFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000072418778&ekey=2208&xpn=CN117918078&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=Dc8j7iM%252FQW1wtnlTbS5ktpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN117918078)\|CN	(CN117918078)\|NAME=INSTITUTE OF GEOCHEMISTRY CHINESE ACADEMY OF SCIENCES , COUNTRY=CN		(CN117918078)\|NAME=ZHANG XIAODONG;Beijing Blue Spider Patent Agency Co., Ltd. , REG=16226		(CN117918078)\|NAME=SHI LIANGXING\|NAME=CENG SIBO\|NAME=LIU ZAIHUA	(CN117918078)\|2	1	1					(CN117918078)\|Number of Claims: NCL=6\|Gazette date: GAZDATE=2024-04-26\|Gazette number: GAZNUM=40-1702\|Number of Pages: NPAGES=8\|		(CN117918078)\|CHINESE (CHI)	(CN117918078)\|Patent	Titre: (CN117918078)\|Method for improving soil and increasing carbon sink Résumé: (CN117918078)\|The invention discloses a method capable of improving soil and increasing carbon sink, and relates to the technical field of soil improvement, the method comprises a crusher and a dolomite raw material, the mined dolomite raw material is put into the crusher to obtain a small-size blocky dolomite raw material, the small-size blocky dolomite raw material is put into a preset grinding machine, and the grinding machine is used for grinding the small-size blocky dolomite raw material; the method comprises the following steps: crushing ground calcium carbonate to obtain powdery ground calcium carbonate, further containing the powdery ground calcium carbonate in an automatic scattering barrel, carrying the automatic scattering barrel through a preset unmanned aerial vehicle, and further uniformly scattering the powdery ground calcium carbonate into an external pretreatment ecological system; calcium carbonate in the ground calcium carbonate is attached to land and is subjected to a weathering reaction with rock, carbon dioxide in air is captured, an associated reaction is generated, and divalent calcium and bicarbonate radicals are obtained through the reaction. The soil conditioner can reduce acidity of soil, is beneficial to soil remediation, increases nutrient elements of the soil, and enhances the soil improvement effect.	24	Abstract	gpt-4o-mini	yes	The method involves the use of dolomite and calcium carbonate to enhance soil, capture CO₂ through weathering reactions, and produce bicarbonates, aligning with the goals of accelerated weathering and carbon sequestration.
28	US61/152,220\|US61/152,220P\|US12/701,156\|WOUS2010/023740	VE2010-000234\|WOUS2010/023740\|IN1897/MUMNP/2011\|MA34162\|ZA201106558\|EG2011081359\|TN2011000396\|BRPI1008447\|EP10741655\|MX2011008525\|UAA201110768\|AU2010213862\|EA201171023\|CN201080016478\|AP2011005878\|IL214555\|CA2752524\|GEAP2010012380\|MYPI2011003742\|PE2011001483\|US12/701,156	BRPI1008447\|GEP20146167\|EP2406353\|MY152266\|MX319678\|UA104616\|EG26451\|AU2010213862\|TN2011000396\|ZA201106558\|US8323481\|VE2010000234\|PE20120704\|EA201171023\|CN102395657\|MA33117\|IN1897/MUMNP/2011\|EP2406353\|MX2011008525\|AP2011005878\|IL214555\|AU2010213862\|WO2010/093684\|CA2752524\|WO2010/093684\|US20100200465	35298	VE2010000234 A 2012-07-26 [VE2010000234]\|WO2010/093684 A3 2010-11-18 [WO201093684]\|WO2010/093684 A2 2010-08-19 [WO201093684]\|IN1897/MUMNP/2011 A 2012-02-03 [IN2011MN01897]\|MA33117 B1 2012-03-01 [MA--33117]\|ZA201106558 B 2013-02-27 [ZA201106558]\|EG26451 A 2013-11-12 [EG--26451]\|TN2011000396 A1 2013-03-27 [TN2011000396]\|BRPI1008447 A2 2019-09-24 [BR201008447]\|EP2406353 A4 2014-09-17 [EP2406353]\|EP2406353 A2 2012-01-18 [EP2406353]\|MX319678 B 2014-04-24 [MX-319678]\|MX2011008525 A 2011-12-16 [MX2011008525]\|UA104616 C2 2014-02-25 [UA-104616]\|AU2010213862 B2 2013-05-02 [AU2010213862]\|AU2010213862 A1 2011-09-22 [AU2010213862]\|EA201171023 A1 2012-03-30 [EA201171023]\|CN102395657 A 2012-03-28 [CN102395657]\|AP2011005878 A0 2011-10-31 [AP2011005878]\|IL214555 A 2011-09-27 [IL-214555]\|CA2752524 A1 2010-08-19 [CA2752524]\|GEP20146167 B 2014-09-25 [GE201406167]\|MY152266 A 2014-09-15 [MY-152266]\|PE20120704 A1 2012-06-27 [PE201200704]\|US8323481 B2 2012-12-04 [US8323481]\|US20100200465 A1 2010-08-12 [US20100200465]	2009-02-12\|2010-02-05\|2010-02-10	2010-02-12\|2010-02-10\|2011-09-10\|2011-09-09\|2011-09-07\|2011-08-11\|2011-08-09\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-05	2019-09-24\|2014-09-25\|2014-09-17\|2014-09-15\|2014-04-24\|2014-02-25\|2013-11-12\|2013-05-02\|2013-03-27\|2013-02-27\|2012-12-04\|2012-07-26\|2012-06-27\|2012-03-30\|2012-03-28\|2012-03-01\|2012-02-03\|2012-01-18\|2011-12-16\|2011-10-31\|2011-09-27\|2011-09-22\|2010-11-18\|2010-08-19\|2010-08-19\|2010-08-12	\|(US8323481)\|2012-12-04\|\|\|(GE201406167)\|2014-09-25\|(MY-152266)\|2014-09-15\|(MX-319678)\|2014-04-24\|(UA-104616)\|2014-02-25\|(EG--26451)\|2013-11-12\|(AU2010213862)\|2013-05-02\|(ZA201106558)\|2013-02-27\|(MA--33117)\|2012-03-01\|\|\|\|\|\|\|\|\|	(EP2406353)\|2015-03-20\|(US8323481)\|2025-01-06\|(WO2010/093684)\|2012-08-12\|(CN102395657)\|2015-01-14\|(GEP20146167)\|2030-02-10\|(MY152266)\|2030-02-10\|(MX319678)\|2030-02-10\|(UA104616)\|2030-02-10\|(EG26451)\|2030-02-10\|(AU2010213862)\|2015-09-03\|(ZA201106558)\|2030-02-10\|(MA33117)\|2030-02-10\|(BRPI1008447)\|2019-10-01\|(TN2011000396)\|2030-02-10\|(VE2010000234)\|2017-07-26\|(PE20120704)\|2016-05-30\|(EA201171023)\|2017-03-30\|(IN1897/MUMNP/2011)\|2022-02-03\|(AP2011005878)\|2016-10-31\|(IL214555)\|2016-09-27\|(CA2752524)\|2016-02-10	(EP2406353)\|Carbon management and sequestration from encapsulated control infrastructures	(EP2406353)\|A method of sequestering carbon dioxide emissions during recovery of hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure (100). This constructed infrastructure (100) defines a substantially encapsulated volume. A comminuted hydrocarbonaceous material can be introduced into the control infrastructure (100) to form a permeable body (120) of hydrocarbonaceous material. The permeable body (120) can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure (100) is a fixed structure. Additionally, during heating, any carbon dioxide that is produced can be sequestered. Removed hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.	RED LEAF RESOURCES	(EP2406353)\|Red Leaf Resources, Inc. ([US])\|(EP2406353)\|Red Leaf Resources, Inc. ([US])\|(US8323481)\|Red Leaf Resources, Inc. ([US])\|(US20100200465)\|DANA TODD\|PATTEN JAMES W\|(WO2010/093684)\|RED LEAF RESOURCES, INC.\|(WO2010/093684)\|RED LEAF RESOURCES, INC. ([US])\|(CN102395657)\|RED LEAF RESOURCES INC. ([US])\|(GEP20146167)\|RED LEAF RESOURCES, INC.\|(MY152266)\|RED LEAF RESOURCES, INC.\|(MX319678)\|RED LEAF RESOURCES INC* ([US])\|(MX2011008525)\|RED LEAF RESOURCES INC*\|(UA104616)\|RED LEAF RESOURCES, INC.\|(EG26451)\|RED LEAF RESOURCES INC\|(AU2010213862)\|Red Leaf Resources, Inc.\|(AU2010213862)\|Red Leaf Resources, Inc.\|(ZA201106558)\|RED LEAF RESOURCES INC\|(MA33117)\|RED LEAF RESOURCES, INC.\|(BRPI1008447)\|Red Leaf Resources, Inc\|(TN2011000396)\|RED LEAF RESOURCES, INC.\|\|(PE20120704)\|RED LEAF RESOURCES, INC.\|\|(IN1897/MUMNP/2011)\|RED LEAF RESOURCES INC ([US])\|(AP2011005878)\|RED LEAF RESOURCES INC\|(IL214555)\|RED LEAF RESOURCES, INC\|(CA2752524)\|RED LEAF RESOURCES, INC. ([US])	DANA TODD\|PATTEN JAMES W	(EP2406353)\|DANA, Todd\|PATTEN, James, W.\|(EP2406353)\|DANA, Todd\|PATTEN, James, W.	(EP2406353)\|Walker, Ross Thomson;Forresters ([DE])\|Reg. Nb: 101298687\|(US8323481)\|Thorpe North & Western LLP\|(WO2010/093684)\|ERICKSEN, Erik S. et al. ([US])\|(CN102395657)\|ZHAO RONGMIN;JEEKAI & PARTNERS\|Reg. Nb: 11245\|(MX319678)\|MARIA ANGELICA PARDAVELL JUAREZ\|(AU2010213862)\|FB Rice ([AU])\|(VE2010000234)\|LINARES ALLOCA MARLIN ENEIDA\|(CA2752524)\|BERESKIN & PARR LLP/S.E.N.C.R.L.,S.R.L. ([CA])	(US8323481)\|As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required.\|Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|In some cases it can be desirable to provide a single type of hydro carbonaceous material so that the permeable body consists essentially of one of the above materials.\|In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants.\|More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body.\|Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like.\|	(US8323481)\|1. A method of sequestering carbon dioxide emissions during recovery of hydrocarbons from hydrocarbonaceous materials comprising: a) forming a constructed permeability control infrastructure which defines a substantially encapsulated volume, said infrastructure comprising clay, bentonite clay, bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, engineered cementitious composites (ECC), fiber reinforced composites, geosynthetic fabrics, sealant, grout, compacted earth, low grade shale, or combinations thereof, wherein the control infrastructure is formed in direct contact with walls of an excavated hydrocarbonaceous material deposit or is freestanding having either a foundation support of earthen material or a local surface topography as a floor; b) introducing a comminuted hydrocarbonaceous material into the control infrastructure to form a permeable body of hydrocarbonaceous material; c) heating the permeable body sufficient to remove hydrocarbons therefrom such that the hydrocarbonaceous material is substantially stationary during heating; d) sequestering carbon dioxide produced during the heating; and e) collecting the removed hydrocarbons.\|	(US8323481)\|In another aspect, walls of the impoundment can be acid, water, and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water.\|In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|In yet another detailed aspect, the permeable body can further comprise an additive or biomass.\|	(US8323481)\|HYDROCARBONACEOUS MATERIAL(100,31)\|HYDROCARBON RECOVERY(100,6)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|BENTONITE AMENDED SOIL(71,3)\|NANOCARBON FULLERENE ADDITIVE(67,2)\|BENTONITE CLAY(53,5)\|GRADE SHALE(43,3)\|SOIL AMENDMENT(43,3)\|GEOSYNTHETIC FABRICS(43,2)\|RESISTANT PVC LINER(40,2)\|SOIL COMPACTION(38,3)\|GEOTEXTILE BAG(38,2)\|ATMOSPHERIC POLLUTANT(38,1)\|METHANEDIONE(37,41)\|SOLVENT RECOVERY(34,2)\|CLAY LINING(33,1)\|SYNTHETIC GEOGRID(32,2)\|COMPACTED FILL(31,6)\|ACID HALIDE(31,1)\|RESIN ION EXCHANGE(31,1)\|METHANEDIONE PRODUCTION(30,1)\|INFRASTRUCTURE(27,25)\|METHANEDIONE PRECIPITATION(27,3)\|CARBONATE DECOMPOSITION(27,2)\|OIL SHALE ORE(27,1)\|SYNTHETIC CLAY(27,1)\|ENCAPSULATED VOLUME(26,20)\|ENORMOUS VOLUME CAPACITY(26,1)\|SUPPORTING FOUNDATION(25,1)\|CONSTRUCTED PERMEABILITY(24,12)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(24,5)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|SEALANT(23,3)\|CO2 EMISSION(23,2)\|POLYMERIC RESIN(23,2)\|TEMPERATURE GEOMEMBRANE(23,1)\|CRYOGENIC PRECIPITATION(22,3)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,3)\|SOLUTION MINING(22,1)\|CONTROL INFRASTRUCTURE(21,24)\|REFRACTORY CEMENT(21,5)\|BRINE SOLUTION(21,1)\|ELECTROPLATING(21,1)\|EXTRACT FLUID(21,1)\|PERMEABILITY(20,25)\|LIQUID METHANEDIONE(20,11)\|GROUT(20,4)\|REBAR(20,4)\|FLOTATION(19,1)\|IMPOUNDMENT WALL(18,12)\|HYDRO CARBONACEOUS MATERIAL(18,6)\|LEACHING(18,1)\|GUIDELINE(17,4)\|REMOVING HYDROCARBON(16,6)\|EARTHEN MATERIAL FOUNDATION SUPPORT(16,1)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(15,10)\|FIBERGLASS(15,4)\|BRINE(15,1)\|CLAY(13,7)\|ENGINEERED CEMENTITIOUS COMPOSITE(13,4)\|BIOMASS(13,3)\|PRECIPITATION(13,3)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|AQUEOUS SOLUTION(12,7)\|ADDITIVE(11,12)\|CEMENT(11,7)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|EARTHEN MATERIAL(11,3)\|FIBER REINFORCED COMPOSITE(11,2)\|DRAIN PIPE(11,1)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|MECHANICAL INTEGRITY(11,1)\|RESISTANCE HEATER(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|INFRASTRUCTURE OPERATING TEMPERATURE(10,1)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|EXTRACTION(9,2)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,12)\|SILICATE(8,3)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|VOID VOLUME(7,7)\|FUEL CELL(7,5)\|MATERIAL DEPOSITION(7,4)\|RADIO FREQUENCY(7,4)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ECONOMIC VALUE(7,1)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|UNDISTURBED GEOLOGICAL FORMATION(6,4)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|ECONOMICALLY COMPETITIVE RECOVERY(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|SALT WATER(5,5)\|PRECIOUS METAL(5,4)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|HYDROCARBON COMBUSTION(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEATING MINED RUBBLE(5,1)\|HEATING RESIDENCE TIME(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|METHANEDIONE COLLECTION(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PERMEABILITY BALANCE(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|HEAT TRANSFER(4,10)\|LIQUID PRODUCT(4,10)\|CASE INTERIOR(4,9)\|HYDROGEN DONOR(4,7)\|HEAVY METAL(4,4)\|BLASTING(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|ECONOMICS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|SURFACE TOPOGRAPHY(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|RECLAMATION(3,2)\|STOICHIOMETRIC CONDITION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|CO2 PRODUCTION(3,1)\|COAL CONTENT(3,1)\|COMMINUTED HYDRO CARBONACEOUS MATERIAL(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|FUTURE DATE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HARVESTED HYDRO CARBONACEOUS MATERIAL(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|INTERIOR CIRCUMSTANCE(3,1)\|INTERIOR HYDROCARBONACEOUS FORMATION(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|LONG HEATING RESIDENCE TIME(3,1)\|MICROBIOLOGY(3,1)\|MINED HYDRO CARBONACEOUS MATERIAL(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|CURVATURE(2,2)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BENTONITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DIFFICULT CHALLENGE(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|FUNCTION VOID SPACE(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|INTERIOR ADDITIVE(2,1)\|INTERIOR CO2(2,1)\|INTERIOR RESIDUAL HYDROCARBON PRODUCT(2,1)\|\|(US20100200465)\|INFRASTRUCTURE(100,25)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDRO CARBONACEOUS MATERIAL(100,8)\|HYDROCARBON RECOVERY(100,6)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|METHANEDIONE COLLECTION(60,4)\|METHANEDIONE(54,49)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,22)\|ATMOSPHERIC POLLUTANT(38,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(34,6)\|SOLVENT RECOVERY(34,2)\|CRYOGENIC PRECIPITATION(33,4)\|CLAY LINING(33,1)\|ACID HALIDE(31,1)\|RESIN ION EXCHANGE(31,1)\|METHANEDIONE PRODUCTION(30,1)\|LIQUID METHANEDIONE(29,13)\|CONTROL INFRASTRUCTURE(28,28)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(28,14)\|IMPOUNDMENT(27,55)\|PERMEABILITY(27,27)\|BENTONITE CLAY(27,3)\|CARBONATE DECOMPOSITION(27,2)\|OIL SHALE ORE(27,1)\|SYNTHETIC CLAY(27,1)\|ENORMOUS VOLUME CAPACITY(26,1)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|CO2 EMISSION(23,2)\|TEMPERATURE GEOMEMBRANE(23,1)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|SOLUTION MINING(22,1)\|HYDROCARBONACEOUS MATERIAL(21,30)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|BRINE SOLUTION(21,1)\|ELECTROPLATING(21,1)\|EXTRACT FLUID(21,1)\|FLOTATION(19,1)\|IMPOUNDMENT WALL(18,12)\|LEACHING(18,1)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|GUIDELINE(17,4)\|REMOVING HYDROCARBON(16,6)\|BRINE(15,1)\|REFRACTORY CEMENT(13,4)\|SILICATE(13,4)\|BIOMASS(13,3)\|PRECIPITATION(13,3)\|SEALANT(13,2)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|ADDITIVE(12,13)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|GROUT(11,3)\|REBAR(11,3)\|DRAIN PIPE(11,1)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|MECHANICAL INTEGRITY(11,1)\|RESISTANCE HEATER(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|INFRASTRUCTURE OPERATING TEMPERATURE(10,1)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|EXTRACTION(9,2)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,11)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|VOID VOLUME(7,7)\|FUEL CELL(7,5)\|MATERIAL DEPOSITION(7,5)\|RADIO FREQUENCY(7,4)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ECONOMIC VALUE(7,1)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|ECONOMICALLY COMPETITIVE RECOVERY(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|LIQUID PRODUCT(5,11)\|PRECIOUS METAL(5,4)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|HYDROCARBON COMBUSTION(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HEATING RESIDENCE TIME(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PERMEABILITY BALANCE(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|HEAT TRANSFER(4,10)\|HYDROGEN DONOR(4,7)\|HEAVY METAL(4,4)\|BLASTING(4,3)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|ECONOMICS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|RECLAMATION(3,2)\|STOICHIOMETRIC CONDITION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|CO2 PRODUCTION(3,1)\|COAL CONTENT(3,1)\|COMMINUTED HYDRO CARBONACEOUS MATERIAL(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|FUTURE DATE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GASEOUS LIGHT HYDROCARBON(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HARVESTED HYDRO CARBONACEOUS MATERIAL(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|LONG HEATING RESIDENCE TIME(3,1)\|MICROBIOLOGY(3,1)\|MINED HYDRO CARBONACEOUS MATERIAL(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DIFFICULT CHALLENGE(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|FUNCTION VOID SPACE(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|\|(CN102395657)\|HYDROCARBONACEOUS MATERIAL(100,39)\|INFRASTRUCTURE(100,24)\|CONSTRUCTED PERMEABILITY(100,13)\|CARBON(100,6)\|HYDROCARBON RECOVERY(100,5)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|METHANEDIONE COLLECTION(48,4)\|METHANEDIONE(45,44)\|ECONOMICALLY COMPETITIVE RECOVERY(39,1)\|ENCAPSULATED VOLUME(31,18)\|METHANEDIONE PRECIPITATE(30,5)\|BENTONITE CLAY(30,1)\|SOLVENT RECOVERY(28,2)\|RESISTIVE HEATER(27,1)\|DEPLETED HYDROCARBONACEOUS MATERIAL(26,14)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(26,7)\|CLAY LINING(26,1)\|CONTROL INFRASTRUCTURE(23,27)\|LIQUID METHANEDIONE(23,13)\|IMPOUNDMENT(22,56)\|ION RESIN EXCHANGE(21,1)\|SYNTHETIC CLAY(21,1)\|INFRASTRUCTURE CONSTRUCTION(19,23)\|CRYOGENIC PRECIPITATION(19,2)\|DRAINAGE PIPE(19,2)\|ECONOMICS(19,1)\|TEMPERATURE GEOMEMBRANE(19,1)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(18,3)\|DIFFICULT CHALLENGE(18,1)\|AQUEOUS SOLUTION(17,10)\|UNDISTURBED GEOLOGICAL FORMATION(17,5)\|BRINE SOLUTION(17,1)\|ELECTROPLATING(17,1)\|SOLUTION MINING(17,1)\|UNDERGROUND MINING(17,1)\|PERMEABILITY(16,29)\|IMPOUNDMENT WALL(15,11)\|ASSURANCE(15,1)\|ENVIRONMENTAL HAZARD(15,1)\|FLOTATION(15,1)\|LEACHING(15,1)\|SEALANT(15,1)\|PERMEABILITY CONTROL IMPOUNDMENT(14,4)\|REMEDIATION(14,2)\|REMOVING HYDROCARBON(13,5)\|SEGMENTED CAPSULE IMPOUNDMENT(13,3)\|BRINE(12,3)\|CONVECTIVE HEATING(12,3)\|BLASTING(12,2)\|CAUSE UNDESIRABLE(12,1)\|FREEZE WALL(11,3)\|PRECIPITATION(11,3)\|RADIO FREQUENCY(11,3)\|REFRACTORY CEMENT(10,4)\|SILICATE(10,4)\|METHANEDIONE SEQUESTRATION(10,3)\|REMOVING PRODUCT(10,1)\|HEATED GAS(9,4)\|GRAVEL(9,3)\|GROUT(9,3)\|REBAR(9,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(9,1)\|CONVECTION(8,4)\|SUPERCRITICAL METHANEDIONE(8,2)\|ACID HALIDE(8,1)\|BIOCHEMICALLY OXIDIZE ORE(8,1)\|HYDROGEN CHLORIDE(8,1)\|MINE CAPSULE IMPOUNDMENT(8,1)\|UNDERGROUND FRESHWATER AQUIFER(8,1)\|MATERIAL DEPOSITION(7,3)\|AFT BERM PERMEABILITY(7,1)\|IMPOUNDMENT CONTAINMENT CAPSULE(7,1)\|HYDROCARBON PRODUCTION(6,11)\|IMPERMEABLE FLOOR(6,3)\|IMPERMEABLE SIDEWALL(6,2)\|NEARBY IMPOUNDMENT(6,2)\|TRILLION BARREL(6,2)\|BENTONITE AMENDED SOIL(6,1)\|ECONOMIC VALUE(6,1)\|SEQUESTERED METHANEDIONE(6,1)\|WOVEN BAMBOO BASKET(6,1)\|FUEL CELL(5,5)\|GUIDELINE(5,4)\|SOIL COMPACTION(5,3)\|MINED CRUSHED STONE(5,2)\|BIOEXTRACTION SCENARIO(5,1)\|CHALLENGING ENDEAVOR(5,1)\|COLLECTIVE IMPOUNDMENT(5,1)\|COMMINUTED AGGLOMERATE(5,1)\|DEEP SALINE AQUIFER(5,1)\|IMPOUNDMENT PERIMETER(5,1)\|INFRASTRUCTURE SHUTDOWN(5,1)\|LANDFILL IMPOUNDMENT(5,1)\|LEAK PROOF EXTRACTION IMPOUNDMENT(5,1)\|METHANE MOLECULE2MOLECULE(5,1)\|NANOCARBON FULLERENE(5,1)\|SEWAGE IMPOUNDMENT(5,1)\|SPRAYED CEMENT SLURRY(5,1)\|SUBDIVIDED IMPOUNDMENT(5,1)\|WATERPROOF QUALITY ENGINEERING(5,1)\|HEAT TRANSFER(4,11)\|LIQUID PRODUCT(4,11)\|GASEOUS PRODUCT(4,4)\|PRECIOUS METAL(4,4)\|IMPOUNDMENT HEIGHT(4,2)\|API MODIFIER(4,1)\|ATMOSPHERIC POLLUTANT(4,1)\|BRINE SATURATED ROCK FORMATION(4,1)\|CANADIAN TAR SAND(4,1)\|CARBONATE DECOMPOSITION(4,1)\|CEMENT REINFORCEMENT(4,1)\|COLLECTED METHANEDIONE(4,1)\|COMPACTED GEOGRID(4,1)\|CONDUIT STRUCTURING(4,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(4,1)\|CONTAINMENT BOUNDARY(4,1)\|CRANE SUSPENDED EXCAVATOR(4,1)\|CRUSHED ORE(4,1)\|DEBT PAYBACK(4,1)\|DECREASING HYDROGENATION(4,1)\|DIRTY FINE PARTICULATE(4,1)\|ECONOMIC VALUATION(4,1)\|EMPTY IMPOUNDMENT(4,1)\|ENGINEERED CARBON REINFORCED GRID(4,1)\|EXCAVATED CAVITY(4,1)\|FIXING METHANEDIONE(4,1)\|GASEOUS HYDROCARBON COMBUSTION HEATER(4,1)\|GEOLOGICAL RESERVOIR ANALYSIS(4,1)\|GEOSYNTHETIC FABRICS(4,1)\|GEOTEXTILE BAG(4,1)\|GRADE CEMENT SLURRY(4,1)\|GRAVITY ASSISTED DRAIN(4,1)\|GRAVITY DRAINAGE PROFILE(4,1)\|HYDROCARBON ENRICHMENT(4,1)\|HYDROCARBON EXCAVATED VOLUME(4,1)\|HYDROCARBON EXCAVATION(4,1)\|HYDROCARBON RICHNESS(4,1)\|HYDROCARBON UNCONTROLLED RELEASE(4,1)\|HYDROCARBONACEOUS DEPOSIT(4,1)\|IMPERMEABLE BARRIER ZONE(4,1)\|IMPERVIOUS BED(4,1)\|IMPOUNDMENT COLLECTION(4,1)\|IMPOUNDMENT FLOOR(4,1)\|IMPOUNDMENT SIDEWALL(4,1)\|INFRASTRUCTURE STABILIZATION(4,1)\|INJECTED CO2THE EFFECTIVE TRAPPING(4,1)\|INSULATION CONTAINMENT(4,1)\|MESSY DUMP(4,1)\|METHANEDIONE ABSORPTION(4,1)\|METHANEDIONE RESOLUTION(4,1)\|MINING AVOIDANCE(4,1)\|MINING HAUL TRUCK(4,1)\|NATIVE BACTERIA(4,1)\|NATURAL DISTRIBUTED COMBUSTOR(4,1)\|NEARBY INFRASTRUCTURE(4,1)\|NONCIRCULAR TUBING(4,1)\|ORE SOLVENT EXTRACTION(4,1)\|PILED RUBBLE(4,1)\|PILLAR MINING(4,1)\|PIT EXCAVATION(4,1)\|PLURAL REFERENT(4,1)\|REFORMING CATALYST(4,1)\|REFORMING ZONE(4,1)\|REGULATORY FLUID MIGRATION REGULATION(4,1)\|REINFORCED CEMENT(4,1)\|REMAINING SHALE DECREASING WETTABILITY(4,1)\|RESISTANT PVC LINER(4,1)\|SHALE MINING(4,1)\|SHELL ICP(4,1)\|SOIL AMENDMENT(4,1)\|SOY INSULATOR(4,1)\|STOICHIOMETRIC COMBUSTION(4,1)\|SUPER DISPOSITION(4,1)\|TAR SAND BITUMEN TREATMENT(4,1)\|TEXTURED BUILT TAIL(4,1)\|THERMALLY DETERIORATED WASTE SHALE(4,1)\|UNCOVERED CAPSULE(4,1)\|UNDERGROUND AQUIFER CONTAMINATION(4,1)\|UNDERGROUND RUBBLE CHANNEL(4,1)\|UNRECOVERED HYDROCARBON(4,1)\|UNUSED RESOURCE(4,1)\|WATERPROOF QUALITY INSULATION(4,1)\|WELLBORE DRILLING(4,1)\|HYDROGEN DONOR(3,7)\|CLAY(3,5)\|HEAVY METAL(3,5)\|MINED MATERIAL(3,5)\|ENZYME(3,4)\|AGITATION(3,3)\|BIOMASS(3,3)\|HEAT PIPE(3,3)\|LIGNITE(3,3)\|MINED HYDROCARBONACEOUS MATERIAL(3,3)\|PYROLYSIS(3,3)\|BIOREMEDIATION(3,2)\|FIXED STRUCTURE(3,2)\|GASEOUS LIGHT HYDROCARBON(3,2)\|HORIZONTAL MINING(3,2)\|OIL BLEND(3,2)\|UNCONTROLLED MIGRATION PREVENTION(3,2)\|ACCEPTED PIPELINE STANDARD(3,1)\|BUILT CAPSULE(3,1)\|CARBON REINFORCING GRID(3,1)\|CERMET COMPOSITE(3,1)\|COLLECTION TROUGH(3,1)\|CONSTRUCTED SULFUR CAPSULE(3,1)\|CONTAINMENT VESSEL SEGMENTATION(3,1)\|CONTAINMENT VESSEL STRUCTURE(3,1)\|DAMAGING STRESS(3,1)\|ECONOMIC FACTOR(3,1)\|EMBEDDED CONDUIT(3,1)\|ENHANCE COMPACTNESS(3,1)\|ENRICHMENT SENSOR(3,1)\|EXPLICITLY RECITED LIMIT(3,1)\|EXTRACTION CAPSULE TREATMENT ZONE(3,1)\|FLOOR LEVELING(3,1)\|FORMATION EXPERIMENTAL MODELING(3,1)\|GAS HEAT SOURCE(3,1)\|GEOPOLITICAL FACTOR(3,1)\|HYDROCARBON BEARING(3,1)\|IMPOUNDMENT DEPTH(3,1)\|IMPOUNDMENT LIFE SPAN(3,1)\|IMPOUNDMENT REGION(3,1)\|LEACHATE PRODUCTION(3,1)\|LEAK PROOF CONTAINMENT VESSEL(3,1)\|LOCALIZED HOTSPOT ELIMINATION(3,1)\|METALLIC ADDITIVE(3,1)\|METHANEDIONE PRODUCTION(3,1)\|MICROBIAL STRAIN(3,1)\|MINERAL LINER(3,1)\|MINING ORE GRADE(3,1)\|MOISTURE MIGRATION(3,1)\|ORE MOISTURE CONTENT(3,1)\|OUTER CAPSULE IMPOUNDMENT(3,1)\|PERFORATED HEATING PIPE(3,1)\|PERMEABILITY BARRIER(3,1)\|PERMEABLE PARTICLE(3,1)\|PIPE CONDENSER(3,1)\|PIPE PERFORATION(3,1)\|PREFABRICATED PIECE(3,1)\|PREFORMED PIECE(3,1)\|PROVEN RESERVOIR(3,1)\|RECOVERY STEAM(3,1)\|REDUCING CO2EMISSIONS(3,1)\|REFRACTORY CEMENT PIPE(3,1)\|REUSABLE PIPE(3,1)\|ROTARY RETORT(3,1)\|SPENT SHALE SOLID RINSING(3,1)\|STAGED CONTAINMENT VESSEL(3,1)\|STAGING PIPE(3,1)\|STORE METHANEDIONE(3,1)\|SUBTERRANEAN TREATMENT ZONE(3,1)\|SUPPLEMENTAL FUEL(3,1)\|SUPPORTIVE IMPOUNDMENT WALL FORMATION(3,1)\|SYNTHETIC GEOGRID(3,1)\|SYNTHETIC NANOCARBON(3,1)\|TAR SAND DEPOSIT(3,1)\|TOXIC EFFLUENT(3,1)\|TUNNELING(3,1)\|ULTRASONIC GENERATOR(3,1)\|VOLATILE HYDROCARBON(3,1)\|HEATING RATE(2,4)\|GEOLOGICAL FORMATION(2,3)\|HEATED FLUID(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|SILO(2,3)\|ADJACENT IMPOUNDMENT(2,2)\|ANCHOR MEMBER(2,2)\|ASPHALTENE(2,2)\|CATHETER(2,2)\|COMBUSTION EXHAUST GAS(2,2)\|COMPACTED FILL TOP(2,2)\|CRUSHING(2,2)\|CULLET(2,2)\|DETONATION(2,2)\|EXPLOSION(2,2)\|FIBERGLASS(2,2)\|HYDROCARBON LIQUID(2,2)\|HYDROGEN CONTENT(2,2)\|INVESTIGATION(2,2)\|POLYCARBONATE(2,2)\|PORTABLE COMBUSTION CHAMBER(2,2)\|RECIRCULATION(2,2)\|RECYCLING(2,2)\|STOICHIOMETRIC CONDITION(2,2)\|SWELLING(2,2)\|VAPOR PRODUCTION(2,2)\|ABUNDANT LIGHT HYDROCARBON(2,1)\|ACROSS MULTIPLE IMPOUNDMENT(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADVENT(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALONE MEET(2,1)\|AMBIENT ENVIRONMENT(2,1)\|ANAEROBIC CONDITION(2,1)\|ANCHOR PILE STRUCTURE(2,1)\|AQUEOUS MUD CONDITION(2,1)\|AROMATICS(2,1)\|ASSAYING(2,1)\|AVAILABLE ADDRESSING(2,1)\|BARRIER MANUFACTURE(2,1)\|BAUXITE(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOGLASS(2,1)\|BIOLEACHING(2,1)\|BITUMEN SOURCE(2,1)\|BLENDING KEROGEN OIL(2,1)\|BYPRODUCT(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPACITY INDICATOR(2,1)\|CATALYTIC GAS(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|CENTRAL GATHERING PIPE(2,1)\|CENTRAL RESERVOIR(2,1)\|CHROMATOGRAPHIC LOCATION(2,1)\|CO2AND(2,1)\|CO2CAN(2,1)\|COAL COMBINATION(2,1)\|COAL CONTENT(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPLEX MACHINERY(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|COMPUTER AIDED MINING(2,1)\|COMPUTER EQUIPMENT(2,1)\|CONCENTRATE(2,1)\|CONCRETE PANEL(2,1)\|CONDENSABILITY(2,1)\|CONDUCTIVE CEMENT(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED GEOMEMBRANE LAYER(2,1)\|CONSTRUCTED IMPOUNDMENT(2,1)\|CONSTRUCTED SULFUR CONTAINMENT VESSEL(2,1)\|CONTAINMENT CONSTRUCTION(2,1)\|CONTAINMENT DISPOSAL AREA(2,1)\|CONTAINMENT VESSEL CONSTRUCTION(2,1)\|CONTAINMENT VOLUME(2,1)\|CONTOUR(2,1)\|CONTROLLED QUALITY SHALE(2,1)\|COOLING FLUID(2,1)\|COOLING PIPE(2,1)\|CRUDE EXTRACTION(2,1)\|CURRENCY(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DEADMAN(2,1)\|DECREASING SULFUR(2,1)\|DECREASING VISCOSITY(2,1)\|DICTATION(2,1)\|DISPERSION FLUID SENSOR(2,1)\|DOWNWARDLY TRANSFERRED LIQUID(2,1)\|DUMPING(2,1)\|DUST PARTICLE(2,1)\|EARTH FORMATION(2,1)\|ECONOMICALLY VIABLE SOURCE(2,1)\|ELECTRICITY(2,1)\|ELECTROLYTE(2,1)\|ELEVATOR(2,1)\|ENCAPSULATED IMPOUNDMENT AREA(2,1)\|ENHANCE REMOVAL(2,1)\|ENHANCER(2,1)\|ENRICHED OIL BEARING ORE(2,1)\|ESTIMATE SOURCE(2,1)\|EXCAVATED HYDROCARBONACEOUS MATERIAL(2,1)\|EXCAVATION AREA(2,1)\|EXPOSED UNDISTURBED GROUND(2,1)\|EXTRACTION PORT(2,1)\|FAST RECOVERY(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE COLLECTION(2,1)\|FINE MESH(2,1)\|FLEXIBLE HOUSING(2,1)\|FLOOR CONSTRUCTION(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID EXTRACTION(2,1)\|FORSTERITE(2,1)\|FRACTURE(2,1)\|FRACTURING(2,1)\|FUNCTIONAL VOID SPACE(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS COMBUSTION(2,1)\|GAS GATHERING(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GAS RELEASE(2,1)\|GASEOUS HYDROCARBON PRODUCT(2,1)\|GEOLOGICAL LOCATION(2,1)\|GEOSYNTHETIC MEMBRANE(2,1)\|HALF ACRE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HAULING(2,1)\|HEAT ABSORPTION(2,1)\|HEATING CONDUIT COST(2,1)\|HEATING CONDUIT LOCATION(2,1)\|HEATING FLUID ISOLATION(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HORIZONTAL BOREHOLE(2,1)\|HOT GAS FILTRATION(2,1)\|HOTSPOT LOCALIZATION(2,1)\|HYDROCARBON VAPOR(2,1)\|HYDROCARBONACEOUS MATERIAL BIOHYDROXYLATION(2,1)\|HYDROCARBONACEOUS MATERIAL COMPACTION(2,1)\|HYDRODESULFURIZATION(2,1)\|HYDROTREAT(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE BOTTOM(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|INFRASTRUCTURE LOCATION(2,1)\|KEROGEN REMOVAL(2,1)\|LARGE CONTAINMENT IMPOUNDMENT(2,1)\|LAYER COMPACTION(2,1)\|LOCALIZED HEATING ZONE(2,1)\|METEOROLOGICAL DATA FACTOR(2,1)\|METHANE STORAGE(2,1)\|METHANEDIONE STORAGE(2,1)\|MINIMAL WASTE(2,1)\|MOLTEN CARBONATE FUEL CELL(2,1)\|MONITORING HEAT(2,1)\|NONHEATED BUFFER ZONE(2,1)\|NONHYDROCARBON(2,1)\|OIL SHALE ORE(2,1)\|OPEN ENDED CAPSULE IMPOUNDMENT(2,1)\|OPTIMIZATION REASON(2,1)\|ORGANIC ADDITIVE(2,1)\|PATHWAY(2,1)\|PIPELINE EXTENSION(2,1)\|PLANT FIBER CELLULOSE(2,1)\|POLYMERIC RESIN(2,1)\|PREVENT ACCIDENTAL LEACHING(2,1)\|PREVENTION MEASURE(2,1)\|PUMPING PIPE(2,1)\|RECOVERING OIL(2,1)\|RECOVERY TREATMENT(2,1)\|RECUPERATOR(2,1)\|REFORMATION(2,1)\|RELEVANT MEASUREMENT(2,1)\|RESIDUAL HYDROCARBON PRODUCT(2,1)\|RETURN DILUENT(2,1)\|ROUND TUBING(2,1)\|SAND PARTICLE(2,1)\|SEQUENTIAL SOLUTION RECOVERY(2,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(2,1)\|SOLVENT SUBSTITUTED COMPOUND(2,1)\|SPRAYED LIQUID EMULSION(2,1)\|STAGED PROCESSING(2,1)\|STEAM INJECTION(2,1)\|STEEL RETORT(2,1)\|STRUCTURED FEATURE(2,1)\|SUPPLEMENTAL HEATING(2,1)\|SUPPORTING BERMS(2,1)\|TECHNICAL CHALLENGE(2,1)\|TRANSFER DEFLATION(2,1)\|TRANSPORT CONDUIT(2,1)\|UNCONTROLLED ESCAPE PREVENTION(2,1)\|UPGRADING(2,1)\|VOLATILE ORGANIC(2,1)\|WATERTIGHT COVER(2,1)\|\|(AU2010213862)\|HYDROCARBONACEOUS MATERIAL(100,35)\|INFRASTRUCTURE(100,30)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDROCARBON RECOVERY(100,5)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|SEQUESTERING METHANEDIONE(66,1)\|METHANEDIONE COLLECTION(60,4)\|METHANEDIONE(51,48)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,22)\|CRYOGENIC PRECIPITATION(33,4)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(32,7)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(31,15)\|LIQUID METHANEDIONE(29,13)\|IMPOUNDMENT(27,53)\|CONTROL INFRASTRUCTURE(26,27)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|PERMEABILITY(20,24)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|REMOVING HYDROCARBON(16,6)\|SILICATE(13,4)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,10)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|MATERIAL DEPOSITION(7,5)\|BENTONITE CLAY(7,2)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|VOID VOLUME(5,4)\|GUIDELINE(5,3)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|LIQUID PRODUCT(4,10)\|HYDROGEN DONOR(4,6)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|CARBONATE DECOMPOSITION(4,1)\|CO2 EMISSION(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|HYDROCARBON COMBUSTION(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|ANTHEM DEGREE(3,2)\|BLASTING(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|PRECIPITATION(3,2)\|RECLAMATION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|COAL CONTENT(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|MICROBIOLOGY(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|VOID SPACE(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOOXIDATION(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ECONOMICS(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|EXCLUSION(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCLUSION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|LIMESTONE(2,1)\|LIMITED COMBUSTION INTENT(2,1)\|LIQUID CONDENSATION(2,1)\|LIQUID EMULSION(2,1)\|LIQUID SOLUTE(2,1)\|LUBRICANT COOLANT(2,1)\|\|(AU2010213862)\|HYDROCARBONACEOUS MATERIAL(100,35)\|INFRASTRUCTURE(100,30)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDROCARBON RECOVERY(100,5)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|SEQUESTERING METHANEDIONE(66,1)\|METHANEDIONE COLLECTION(60,4)\|METHANEDIONE(51,48)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,22)\|CRYOGENIC PRECIPITATION(33,4)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(32,7)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(31,15)\|LIQUID METHANEDIONE(29,13)\|IMPOUNDMENT(27,53)\|CONTROL INFRASTRUCTURE(26,27)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|PERMEABILITY(20,24)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|REMOVING HYDROCARBON(16,6)\|SILICATE(13,4)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,10)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|MATERIAL DEPOSITION(7,5)\|BENTONITE CLAY(7,2)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|VOID VOLUME(5,4)\|GUIDELINE(5,3)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|LIQUID PRODUCT(4,10)\|HYDROGEN DONOR(4,6)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|CARBONATE DECOMPOSITION(4,1)\|CO2 EMISSION(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|HYDROCARBON COMBUSTION(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|ANTHEM DEGREE(3,2)\|BLASTING(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|PRECIPITATION(3,2)\|RECLAMATION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|COAL CONTENT(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|MICROBIOLOGY(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|VOID SPACE(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOOXIDATION(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ECONOMICS(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|EXCLUSION(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCLUSION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|LIMESTONE(2,1)\|LIMITED COMBUSTION INTENT(2,1)\|LIQUID CONDENSATION(2,1)\|LIQUID EMULSION(2,1)\|LIQUID SOLUTE(2,1)\|LUBRICANT COOLANT(2,1)\|\|(IN1897/MUMNP/2011)\|HYDROCARBONACEOUS MATERIAL(100,35)\|INFRASTRUCTURE(100,25)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDROCARBON RECOVERY(100,5)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|METHANEDIONE COLLECTION(66,3)\|METHANEDIONE(54,50)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,21)\|CRYOGENIC PRECIPITATION(33,4)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(32,7)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(31,15)\|LIQUID METHANEDIONE(29,13)\|IMPOUNDMENT(27,52)\|CONTROL INFRASTRUCTURE(26,27)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|PERMEABILITY(19,23)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|REMOVING HYDROCARBON(16,6)\|SILICATE(13,4)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,10)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|MATERIAL DEPOSITION(7,5)\|BENTONITE CLAY(7,2)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|VOID VOLUME(5,4)\|GUIDELINE(5,3)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|LIQUID PRODUCT(4,10)\|HYDROGEN DONOR(4,6)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|CARBONATE DECOMPOSITION(4,1)\|CO2 EMISSION(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|HYDROCARBON COMBUSTION(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|BIOMASS(3,3)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|BLASTING(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|PRECIPITATION(3,2)\|RECLAMATION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|CO2 PRODUCTION(3,1)\|COAL CONTENT(3,1)\|COLLECTION UNIT OPERATIVE IY(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|MICROBIOLOGY(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|VOID SPACE(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ECONOMICS(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GEOMEMBRANE(2,1)\|GUARANTEE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|LIMESTONE(2,1)\|LIMITED COMBUSTION INTENT(2,1)\|LIQUID CONDENSATION(2,1)\|LIQUID EMULSION(2,1)\|LIQUID SOLUTE(2,1)\|LUBRICANT COOLANT(2,1)\|MATERIAL UNCONTROLLED MIGRATION(2,1)\|\|(CA2752524)\|HYDROCARBONACEOUS MATERIAL(100,36)\|INFRASTRUCTURE(100,25)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDROCARBON RECOVERY(100,5)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|METHANEDIONE COLLECTION(60,4)\|METHANEDIONE(54,49)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,22)\|CRYOGENIC PRECIPITATION(33,4)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(32,7)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(31,15)\|LIQUID METHANEDIONE(29,13)\|IMPOUNDMENT(27,54)\|CONTROL INFRASTRUCTURE(26,27)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|PERMEABILITY(20,24)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|REMOVING HYDROCARBON(16,6)\|SILICATE(13,4)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,10)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|MATERIAL DEPOSITION(7,5)\|BENTONITE CLAY(7,2)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|VOID VOLUME(5,4)\|GUIDELINE(5,3)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|LIQUID PRODUCT(4,10)\|HYDROGEN DONOR(4,6)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|CARBONATE DECOMPOSITION(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|HYDROCARBON COMBUSTION(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|BLASTING(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|PRECIPITATION(3,2)\|RECLAMATION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|COAL CONTENT(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|MICROBIOLOGY(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|VOID SPACE(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOOXIDATION(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ECONOMICS(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|LIMESTONE(2,1)\|LIMITED COMBUSTION INTENT(2,1)\|LIQUID CONDENSATION(2,1)\|LIQUID EMULSION(2,1)\|LIQUID SOLUTE(2,1)\|LUBRICANT COOLANT(2,1)\|MATERIAL UNCONTROLLED MIGRATION(2,1)\|	(US8323481)\|What is claimed is:\|1. A method of sequestering carbon dioxide emissions during recovery of hydrocarbons from hydrocarbonaceous materials comprising:\| a) forming a constructed permeability control infrastructure which defines a substantially encapsulated volume, said infrastructure comprising clay, bentonite clay, bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, engineered cementitious composites (ECC), fiber reinforced composites, geosynthetic fabrics, sealant, grout, compacted earth, low grade shale, or combinations thereof, wherein the control infrastructure is formed in direct contact with walls of an excavated hydrocarbonaceous material deposit or is freestanding having either a foundation support of earthen material or a local surface topography as a floor;\| b) introducing a comminuted hydrocarbonaceous material into the control infrastructure to form a permeable body of hydrocarbonaceous material;\| c) heating the permeable body sufficient to remove hydrocarbons therefrom such that the hydrocarbonaceous material is substantially stationary during heating;\| d) sequestering carbon dioxide produced during the heating; and e) collecting the removed hydrocarbons.\|2. The method of claim 1, wherein sequestering carbon dioxide is achieved by reacting carbon dioxide with an aqueous solution to form a precipitation of carbon dioxide with a metal.\|3. The method of claim 2, wherein the metal is selected from the group consisting of calcium, magnesium, oxides thereof, silicates thereof, and mixtures thereof.\|4. The method of claim 2, wherein the aqueous solution is salt water.\|5. The method of claim 1, wherein sequestering carbon dioxide is achieved by injecting exhausted hydro carbonaceous materials with the carbon dioxide and salt water.\|6. The method of claim 1, wherein sequestering carbon dioxide is achieved by cryogenic precipitation forming liquid carbon dioxide.\|7. The method of claim 6, wherein the liquid carbon dioxide is mixed with exhausted hydrocarbonaceous materials.\|8. The method of claim 1, wherein sequestering carbon dioxide is achieved by injecting exhausted hydrocarbonaceous materials with the carbon dioxide.\|9. The method of claim 8, wherein the injecting is performed with a catalyst.\|10. The method of claim 1, wherein the step of heating includes injecting heated gases into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body.\|11. The method of claim 1, wherein the permeable body further comprises a plurality of conduits embedded within the permeable body, at least some of said conduits being configured as heating pipes.\|12. The method of claim 1, wherein the infrastructure comprises clay, bentonite clay, bentonite amended soil, compacted fill, compacted earth, low grade shale, or combinations thereof.	(US8323481)\|RELATED APPLICATION\|[0001] This application claims priority to U.S. Provisional Patent Application No. 61/152,220 filed Feb. 12, 2009 which is incorporated herein by reference.\|(US8323481)\|BACKGROUND\|[0002] Global and domestic demand for fossil fuels continues to rise despite price increases and other economic and geopolitical concerns. As such demand continues to rise, research and investigation into finding additional economically viable sources of fossil fuels correspondingly increases. Historically, many have recognized the vast quantities of energy stored in oil shale, coal and tar sand deposits, for example. However, these sources remain a difficult challenge in terms of economically competitive recovery. Canadian tar sands have shown that such efforts can be fruitful, although many challenges still remain, including environmental impact, product quality, production costs and process time, among others.\|[0003] Estimates of world-wide oil shale reserves range from two to almost seven trillion barrels of oil, depending on the estimating source. Regardless, these reserves represent a tremendous volume and remain a substantially untapped resource. A large number of companies and investigators continue to study and test methods of recovering oil from such reserves. In the oil shale industry, methods of extraction have included underground rubble chimneys created by explosions, in-situ methods such as In-Situ Conversion Process (ICP) method (Shell Oil), and heating within steel fabricated retorts. Other methods have included in-situ radio frequency methods (microwaves), and “modified” in-situ processes wherein underground mining, blasting and retorting have been combined to make rubble out of a formation to allow for better heat transfer and product removal.\|[0004] Among typical oil shale processes, all face tradeoffs in economics and environmental concerns. No current process alone satisfies economic, environmental, and technical challenges. Moreover, global warming concerns give rise to additional measures to address carbon dioxide (CO2) emissions which are associated with such processes. Methods are needed that accomplish environmental stewardship, yet still provide high-volume cost-effective oil production.\|[0005] Below ground in-situ concepts emerged based on their ability to produce high volumes while avoiding the cost of mining. While the cost savings resulting from avoiding mining can be achieved, the in-situ method requires heating a formation for a longer period of time due to the extremely low thermal conductivity and high specific heat of solid oil shale. Perhaps the most significant challenge for any in-situ process is the uncertainty and long term potential of water contamination that can occur with underground freshwater aquifers. In the case of Shell's ICP method, a “freeze wall” is used as a barrier to keep separation between aquifers and an underground treatment area. Although this is possible, no long term analysis has proven for extended periods to guarantee the prevention of contamination. Without guarantees and with even fewer remedies should a freeze wall fail, other methods are desirable to address such environmental risks.\|[0006] For this and other reasons, the need remains for methods and systems which can provide improved recovery of hydrocarbons from suitable hydrocarbon-containing materials, which have acceptable economics and avoid the drawbacks mentioned above.\|SUMMARY\|[0007] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating the hydrocarbonaceous material can be substantially stationary. Additionally, during heating, any carbon dioxide that is produced can be sequestered. Removed hydrocarbons can be collected for further processing, use in the process as supplemental fuel or additives, and/or direct use without further treatment.\|[0008] Additional features and advantages of these principles will be apparent from the following detailed description, which illustrates, by way of example, features of the invention.\|(US8323481)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0009] FIG. 1 is side partial cutaway view schematic of a constructed permeability control infrastructure in accordance with one embodiment.\|[0010] FIGS. 2A and 2B are top and plan views of a plurality of permeability control impoundments in accordance with one embodiment.\|[0011] FIG. 3 is a side cutaway view of a permeability control impoundment in accordance with one embodiment.\|[0012] FIG. 4 is a schematic of a portion of a constructed infrastructure in accordance with an embodiment.\|[0013] FIG. 5 is a schematic showing heat transfer between two permeability control impoundments in accordance with another embodiment.\|(US8323481)\|DETAILED DESCRIPTION\|[0014] It should be noted that the figures are merely exemplary of several embodiments and no limitations on the scope of the present invention are intended thereby. Further, the figures are generally not drawn to scale, but are drafted for purposes of convenience and clarity in illustrating various aspects of the invention.\|DETAILED DESCRIPTION\|[0015] Reference will now be made to exemplary embodiments and specific language will be used herein to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended. Alterations and further modifications of the inventive features described herein, and additional applications of the principles of the invention as described herein, which would occur to one skilled in the relevant art and having possession of this disclosure, are to be considered within the scope of the invention. Further, before particular embodiments are disclosed and described, it is to be understood that this invention is not limited to the particular process and materials disclosed herein as such may vary to some degree. It is also to be understood that the terminology used herein is used for the purpose of describing particular embodiments only and is not intended to be limiting, as the scope of the present invention will be defined only by the appended claims and equivalents thereof.\|DEFINITIONS\|[0016] In describing and claiming the present invention, the following terminology will be used.\|[0017] The singular forms “a,” “an,” and “the” include plural references unless the context clearly dictates otherwise. Thus, for example, reference to “a wall” includes reference to one or more of such structures, “a permeable body” includes reference to one or more of such materials, and “a heating step” refers to one or more of such steps.\|[0018] As used herein “existing grade” or similar terminology refers to the grade or a plane parallel to the local surface topography of a site containing an infrastructure as described herein which infrastructure may be above or below the existing grade.\|[0019] As used herein, “conduits” refers to any passageway along a specified distance which can be used to transport materials and/or heat from one point to another point. Although conduits can generally be circular pipes, other non-circular conduits can also be useful. Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|[0020] As used herein, “constructed infrastructure” refers to a structure which is substantially entirely man made, as opposed to freeze walls, sulfur walls, or other barriers which are formed by modification or filling pores of an existing geological formation.\|[0021] The constructed permeability control infrastructure is often substantially free of undisturbed geological formations, although the infrastructure can be formed adjacent or in direct contact with an undisturbed formation. Such a control infrastructure can be unattached or affixed to an undisturbed formation by mechanical means, chemical means, or a combination of such means, e.g. bolted into the formation using anchors, ties, or other suitable hardware.\|[0022] As used herein, “comminuted” refers to breaking a formation or larger mass into pieces. A comminuted mass can be rubbilized or otherwise broken into fragments.\|[0023] As used herein, “hydrocarbonaceous material” refers to any hydrocarbon-containing material from which hydrocarbon products can be extracted or derived. For example, hydrocarbons may be extracted directly as a liquid, removed via solvent extraction, directly vaporized or otherwise removed from the material. However, many hydro carbonaceous materials contain kerogen or bitumen which is converted to a hydrocarbon through heating and pyrolysis. Hydrocarbonaceous materials can include, but is not limited to, oil shale, tar sands, coal, lignite, bitumen, peat, and other organic materials.\|[0024] As used herein, “impoundment” refers to a structure designed to hold or retain an accumulation of fluid and/or solid moveable materials. An impoundment generally derives at least a substantial portion of foundation and structural support from earthen materials. Thus, the control walls do not always have independent strength or structural integrity apart from the earthen material and/or formation against which they are formed.\|[0025] As used herein, “permeable body” refers to any mass of comminuted hydro carbonaceous material having a relatively high permeability which exceeds permeability of a solid undisturbed formation of the same composition. Suitable permeable bodies can have greater than about 10% void space and typically have void space from about 30% to 45%, although other ranges may be suitable. Allowing for high permeability facilitates, for example, through the incorporation of large irregularly shaped particles, heating of the body through convection as the primary heat transfer while also substantially reducing costs associated with crushing to very small sizes, e.g. below about 1 to about 0.5 inch.\|[0026] As used herein, “wall” refers to any constructed feature having a permeability control contribution to confining material within an encapsulated volume defined at least in part by control walls. Walls can be oriented in any manner such as vertical, although ceilings, floors, and other contours defining the encapsulated volume can also be “walls” as used herein.\|[0027] As used herein, “mined” refers to a material which has been removed or disturbed from an original stratographic or geological location to a second and different location or returned to the same location. Typically, mined material can be produced by rubbilizing, crushing, explosively detonating, or otherwise removing material from a geologic formation.\|[0028] As used herein, “adsorb,” “adsorbing,” or “adsorbed” refers to the process where a gas or liquid solute accumulates on the surface of a solid or a liquid or diffuses into a solid or liquid. Generally, when referring to carbon dioxide, the carbon dioxide is adsorbed into a material such that the carbon dioxide is substantially immobilized.\|[0029] As used herein, “substantially stationary” refers to nearly stationary positioning of materials with a degree of allowance for subsidence, expansion, and/or settling as hydrocarbons are removed from the hydrocarbonaceous material from within the enclosed volume to leave behind lean material. In contrast, any circulation and/or flow of hydrocarbonaceous material such as that found in fluidized beds or rotating retorts involves highly substantial movement and handling of hydrocarbonaceous material.\|[0030] As used herein, “substantial” when used in reference to a quantity or amount of a material, or a specific characteristic thereof, refers to an amount that is sufficient to provide an effect that the material or characteristic was intended to provide. The exact degree of deviation allowable may in some cases depend on the specific context. Similarly, “substantially free of” or the like refers to the lack of an identified element or agent in a composition. Particularly, elements that are identified as being “substantially free of” are either completely absent from the composition, or are included only in amounts which are small enough so as to have no measurable effect on the composition.\|[0031] As used herein, “about” refers to a degree of deviation based on experimental error typical for the particular property identified. The latitude provided the term “about” will depend on the specific context and particular property and can be readily discerned by those skilled in the art. The term “about” is not intended to either expand or limit the degree of equivalents which may otherwise be afforded a particular value. Further, unless otherwise stated, the term “about” shall expressly include “exactly,” consistent with the discussion below regarding ranges and numerical data.\|[0032] Concentrations, dimensions, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of about 1 to about 200 should be interpreted to include not only the explicitly recited limits of 1 and 200, but also to include individual sizes such as 2, 3, 4, and sub-ranges such as 10 to 50, 20 to 100, etc.\|[0033] As used herein, a plurality of items, structural elements, compositional elements, and/or materials may be presented in a common list for convenience. However, these lists should be construed as though each member of the list is individually identified as a separate and unique member. Thus, no individual member of such list should be construed as a de facto equivalent of any other member of the same list solely based on their presentation in a common group without indications to the contrary.\|[0034] Carbon Management and Sequestration from Control Infrastructures\|[0035] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined or harvested hydro carbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure is a fixed structure. Additionally, during heating, at least a portion of carbon dioxide that is produced can be sequestered. Removed fluid hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.\|[0036] The constructed permeability control infrastructure can be formed using existing grade as floor support and/or as side wall support for the constructed infrastructure. For example, the control infrastructure can be formed as a free standing structure, i.e. using only existing grade as a floor with side walls being man-made. Alternatively, the control infrastructure can be formed within an excavated pit. Regardless, the control infrastructures are always formed above-grade.\|[0037] A constructed permeability control infrastructure can include a permeability control impoundment which defines a substantially encapsulated volume. The permeability control impoundment is substantially free of undisturbed geological formations. Specifically, the permeability control aspect of the impoundment can be completely constructed and manmade as a separate isolation mechanism for prevention of uncontrolled migration of material into or out of the encapsulated volume.\|[0038] In one embodiment, the permeability control impoundment can be formed along walls of an excavated hydrocarbonaceous material deposit. For example, oil shale, tar sands, or coal can be mined from a deposit to form a cavity which corresponds approximately to a desired encapsulation volume for an impoundment. The excavated cavity can then be used as a form and support to create the permeability control impoundment.\|[0039] In one alternative aspect, at least one additional excavated hydrocarbonaceous material deposit can be formed such that a plurality of impoundments can be operated. Further, such a configuration can facilitate a reduction in transportation distance of the mined material. Specifically, the mined hydro carbonaceous material for any particular encapsulated volume can be mined from an adjacent excavated hydrocarbonaceous material deposit. In this manner, a grid of constructed structures can be built such that mined material can be immediately and directly filled into an adjacent impoundment.\|[0040] Mining and/or excavation of hydrocarbonaceous deposits can be accomplished using any suitable technique. Conventional surface mining can be used, although alternative excavators can also be used without requirement of transportation of the mined materials. In one specific embodiment, the hydrocarbonaceous deposit can be excavated using a crane-suspended excavator. One example of a suitable excavator can include vertical tunnel boring machines. Such machines can be configured to excavate rock and material beneath the excavator. As material is removed, the excavator is lowered to ensure substantially continuous contact with a formation. Removed material can be conveyed out of the excavation area using conveyors or lifts. Alternatively, the excavation can occur under aqueous slurry conditions to reduce dust problems and act as a lubricant/coolant. The slurry material can be pumped out of the excavation for separation of solids in a settling tank or other similar solid-liquid separator, or the solids may be allowed to precipitate directly in an impoundment. This approach can be readily integrated with simultaneous or sequential solution-based recovery of metals and other materials as described in more detail below.\|[0041] Further, excavation and formation of a permeability control impoundment can be accomplished simultaneously. For example, an excavator can be configured to remove hydrocarbonaceous material while side walls of an impoundment are formed. Material can be removed from just underneath edges of the side walls such that the walls can be guided downward to allow additional wall segments to be stacked above. This approach can allow for increased depths while avoiding or reducing dangers of cave-in prior to formation of supporting impoundment walls.\|[0042] The impoundment can be formed of any suitable material which provides isolation of material transfer across walls of the impoundment. In this manner, integrity of the walls is retained during operation of the control infrastructure sufficient to substantially prevent uncontrolled migration of fluids outside of the control infrastructure. Non-limiting examples of suitable material for use in forming the impoundment of the constructed permeability control infrastructure can include clay, bentonite clay (e.g. clay comprising at least a portion of bentonite), bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, or combinations thereof. Engineered cementitious composites (ECC) materials, fiber reinforced composites, and the like can be particularly strong and can be readily engineered to meet permeability and temperature tolerance requirements of a given installation. As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required. For example, materials having a melting point above the maximum operating temperature of the infrastructure can be useful to maintain containment during and after heating and recovery. However, lower temperature materials can also be used if a non-heated buffer zone is maintained between the walls and heated portions of the permeable body. Such buffer zones can range from 6 inches to 50 feet depending on the particular material used for the impoundment and the composition of the permeable body. In another aspect, walls of the impoundment can be acid, water, and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water. For impoundment walls formed along formations or other solid support, the impoundment walls can be formed of a sprayed grouting, sprayed liquid emulsions, or other sprayed material such as sprayable refractory grade grouting which forms a seal against the formation and creates the permeability control wall of the impoundments. Impoundment walls may be substantially continuous such that the impoundment defines the encapsulated volume sufficiently to prevent substantial movement of fluids into or out of the impoundment other than defined inlets and outlets, e.g. via conduits or the like as discussed herein. In this manner, the impoundments can readily meet government fluid migration regulations. Alternatively, or in combination with a manufactured barrier, portions of the impoundment walls can be undisturbed geological formation and/or compacted earth. In such cases, the constructed permeability control infrastructure is a combination of permeable and impermeable walls as described in more detail below.\|[0043] In one detailed aspect, a portion of hydro carbonaceous material, either pre- or post-processed, can be used as a cement fortification and/or cement base which are then poured in place to form portions or the entirety of walls of the control infrastructure. These materials can be formed in place or can be preformed and then assembled on site to form an integral impoundment structure. For example, the impoundment can be constructed by cast forming in place as a monolithic body, extrusion, stacking of preformed or precast pieces, concrete panels joined by a grout (cement, ECC, or other suitable material), inflated form, or the like. The forms can be built up against a formation or can be stand alone structures. Forms can be constructed of any suitable material such as, but not limited to, steel, wood, fiberglass, polymer, or the like. The forms can be assembled in place or may be oriented using a crane or other suitable mechanism. Alternatively, the constructed permeability control infrastructure can be formed of gabions and/or geosynthetic fabrics assembled in layers with compacted fill material. Optional binders can be added to enhance compaction of the permeability control walls. In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|[0044] Impoundment walls can optionally include non-permeable insulation and/or fines collection layers. These permeable layers can be oriented between the permeability control barrier and the permeable body. For example, a layer of hydrocarbonaceous comminuted material can be provided which allows fluids to enter, cool, and at least partially condense within the layer. Such permeable layer material can generally have a particle size smaller than the permeable body. Further, such hydrocarbonaceous material can remove fines from passing fluids via various attractive forces. In one embodiment, the construction of impoundment walls and floors can include multiple compacted layers of indigenous or manipulated low grade shale with any combination of sand, cement, fiber, plant fiber, nano carbons, crushed glass, reinforcement steel, engineered carbon reinforcement grid, calcium salts, and the like. In addition to such composite walls, designs which inhibit long term fluid and gas migration through additional impermeability engineering can be employed including, but not limited to, liners, geo-membranes, compacted soils, imported sand, gravel or rock and gravity drainage contours to move fluids and gases away from impervious layers to egress exits. Impoundment floor and wall construction, can, but need not comprise, a stepped up or stepped down slope or bench as the case of mining course may dictate following the optimal ore grade mining. In any such stepped up or down applications, floor leveling and containment wall construction can typically drain or slope to one side or to a specific central gathering area(s) for removal of fluids by gravity drainage assistance.\|[0045] Optionally, capsule wall and floor construction can include insulation which prevents heat transfer outside of the constructed infrastructure or outside of inner capsules or conduits within the primary constructed capsule containment. Insulation can comprise manufactured materials, cement or various materials other materials which are less thermally conductive than surrounding masses, i.e. permeable body, formation, adjacent infrastructures, etc. Thermally insulating barriers can also be formed within the permeable body, along impoundment walls, ceilings, and/or floors. One detailed aspect includes the use of biodegradable insulating materials, e.g. soy insulation and the like. This is consistent with embodiments wherein the impoundment is a single use system such that insulations, pipes, and/or other components can have a relatively low useful life, e.g. less than 1-2 years. This can reduce equipment costs as well as reduce long-term environmental impact.\|[0046] These structures and methods can be applied at almost any scale. Larger encapsulated volumes and increased numbers of impoundments can readily produce hydrocarbon products and performance comparable to or exceeding smaller constructed infrastructures. As an illustration, single impoundments can range in size from tens of meters across to tens of acres. Optimal impoundment sizes may vary depending on the hydrocarbonaceous material and operating parameters, however it is expected that suitable areas can range from about one-half to five acres in top plan surface area.\|[0047] The methods and infrastructures can be used for recovery of hydrocarbons from a variety of hydrocarbonaceous materials. One particular advantage is a wide degree of latitude in controlling particle size, conditions, and composition of the permeable body introduced into the encapsulated volume. Non-limiting examples of mined hydrocarbonaceous material which can be treated comprise oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof. In some cases it can be desirable to provide a single type of hydro carbonaceous material so that the permeable body consists essentially of one of the above materials. However, the permeable body can include mixtures of these materials such that grade, oil content, hydrogen content, permeability and the like can be adjusted to achieve a desired result. Further, different hydrocarbon materials can be placed in multiple layers or in a mixed fashion such as combining coal, oil shale, tar sands, biomass, and/or peat.\|[0048] In one embodiment, hydrocarbon containing material can be classified into various inner capsules within a primary constructed infrastructure for optimization reasons. For instance, layers and depths of mined oil shale formations may be richer in certain depth pay zones as they are mined. Once blasted, mined, shoveled, and hauled inside of capsule for placement, richer oil bearing ores can be classified or mixed by richness for optimal yields, faster recovery, or for optimal averaging within each impoundment. Further, providing layers of differing composition can have added benefits. For example, a lower layer of tar sands can be oriented below an upper layer of oil shale. Generally, the upper and lower layers can be in direct contact with one another although this is not required. The upper layer can include heating pipes embedded therein as described in more detail below. The heating pipes can heat the oil shale sufficient to liberate kerogen oil, including short-chain liquid hydrocarbons, which can act as a solvent for bitumen removal from the tar sands. In this manner, the upper layer acts as an in situ solvent source for enhancing bitumen removal from the lower layer. Heating pipes within the lower layer are optional such that the lower layer can be free of heating pipes or may include heating pipes, depending on the amount of heat transferred via downward passing liquids from the upper layer and any other heat sources. The ability to selectively control the characteristics and composition of the permeable body adds a significant amount of freedom in optimizing oil yields and quality.\|[0049] Furthermore, in many embodiments, the liberated gaseous and liquid products act as an in situ produced solvent which supplements kerogen removal and/or additional hydrocarbon removal from the hydrocarbonaceous material.\|[0050] In yet another detailed aspect, the permeable body can further comprise an additive or biomass. Additives can include any composition which acts to increase the quality of removed hydrocarbons, e.g. increased API, decreased viscosity, improved flow properties, reduced wetting of residual shale, reduction of sulfur, hydrogenation agents, etc. Non-limiting examples of suitable additives can include bitumen, kerogen, propane, natural gas, natural gas condensate, crude oil, refining bottoms, asphaltenes, common solvents, other diluents, and combinations of these materials. In one specific embodiment, the additive can include a flow improvement agent and/or a hydrogen donor agent. Some materials can act as both or either agents to improve flow or as a hydrogen donor. Non-limiting examples of such additives can include methane, natural gas condensates, common solvent such as acetone, toluene, benzene, etc., and other additives listed above. Additives can act to increase the hydrogen to carbon ratio in any hydrocarbon products, as well as act as a flow enhancement agent. For example, various solvents and other additives can create a physical mixture which has a reduced viscosity and/or reduced affinity for particulate solids, rock, and the like. Further, some additives can chemically react with hydrocarbons and/or allow liquid flow of the hydrocarbon products. Any additives used can become part of a final recovered product or can be removed and reused or otherwise disposed of.\|[0051] Similarly, biological hydroxylation of hydrocarbonaceous materials to form synthetic gas or other lighter weight products can be accomplished using known additives and approaches. Enzymes or biocatalysts can also be used in a similar manner. Further, manmade materials can also be used as additives such as, but not limited to, tires, polymeric refuse, or other hydrocarbon-containing materials.\|[0052] Although these methods are broadly applicable, as a general guideline, the permeable body can include particles from about ⅛ inch to about 6 feet in largest dimension, and in some cases less than 1 foot and in other cases less than about 6 inches. However, as a practical matter, sizes from about 2 inches to about 2 feet can provide good results with about 1 foot diameter being useful for oil shale especially. Void space can be an important factor in determining optimal particle diameters. As a general matter, any functional void space can be used; however, about 10% to about 50% and in some cases about 30% to about 45% usually provides a good balance of permeability and effective use of available volumes. Void volumes can be varied somewhat by varying other parameters such as heating conduit placement, additives, and the like. Mechanical separation of mined hydrocarbonaceous materials allows creation of fine mesh, high permeability particles which enhance thermal dispersion rates once placed in capsule within the impoundment. The added permeability allows for more reasonable, low temperatures which also help to avoid higher temperatures which result in greater CO2 production from carbonate decomposition and associated release of trace heavy metals, volatile organics, and other compounds which can create toxic effluent and/or undesirable materials which are monitored and controlled.\|[0053] Carbon dioxide that is produced during the recovery process can be sequestered using one or more approaches. In particular, carbon dioxide can be converted to a solid or liquid form such that the associated carbon is precipitated or otherwise converted to a useful product. Such sequestering can be optionally accomplished by reacting carbon dioxide with an aqueous solution to form a precipitation of carbon dioxide with a metal. When referring to carbon dioxide precipitates or precipitating carbon dioxide, it is understood that precipitation consumes the carbon dioxide such that the carbon dioxide no longer exists as a CO2 structure. As such, the process is generally irreversible and differs from general adsorption techniques, which can also be used for sequestering carbon dioxide as further described herein. In one embodiment, the aqueous solution can be an ionic solution. In another embodiment, the aqueous solution can be salt water. The metal can be any metal that is capable of forming a solid with carbon dioxide including oxides thereof. In one embodiment, the metal can be calcium, magnesium, including oxides thereof, silicates thereof, and mixtures thereof. In one embodiment, the metal can be in the form of forsterite, serpentine and/or peridotite. In one embodiment, the exhausted hydrocarbonaceous materials can be injected or admixed with the carbon dioxide and salt water to form carbon dioxide precipitates. Such a process can take advantage of metals found in the exhausted hydrocarbonaceous materials.\|[0054] Additionally, other materials can be added to increase the reaction kinetics to form the carbon dioxide precipitate. For example, the addition of acids, catalysts, or other organic compounds may increase the reaction kinetics. Such sequestering can also produce heat during the sequestering process. In one embodiment, the heat can be redirected and applied to the heating step as discussed herein. Such recycling of heat can further provide a more efficient recovery system.\|[0055] Additionally, or alternatively, sequestering of carbon dioxide can be achieved by cryogenic precipitation forming liquid carbon dioxide. The collected carbon dioxide can be liquefied by lowering the temperature. Such liquid carbon dioxide can then be transferred to a container for disposal or for reuse. In one embodiment, the liquid carbon dioxide can be reacted to form polycarbonates, which can provide a stable form for disposal or potential use in other industries. In another embodiment, the liquid carbon dioxide can be used to further process the exhausted hydrocarbonaceous materials, as further discussed herein, including rinsing the hydrocarbonaceous materials during the recovery process. Such treatment can provide additional recovery of hydrocarbons that have not been removed during the initial recovery process as described herein.\|[0056] The sequestered carbon dioxide can be used in other commercial processes. In one embodiment, carbon dioxide can be used to isolate polymers from fluids. For example, carbon dioxide can be used to isolate polycarbonates from a solvent, e.g. methylene chloride. In another embodiment, carbon dioxide can be pumped into depleted permeable bodies. In the case of permeable bodies having a high coal content, once the initial stores of methane or other products are recovered, CO2 can be pumped into the impoundment, where it is stored in the coal, which can then provide the benefit of releasing additional methane. Between three and thirteen molecules of CO2 can be absorbed for each molecule of methane, making coal an excellent storage location for CO2.\|[0057] In one embodiment, storage of carbon dioxide can be performed in deep saline aquifers or brine-saturated rock formations that occur deep underground or under the ocean. Specifically, wells deep underground consisting of porous rock, such as limestone or sandstone, saturated with saltwater can form an effective trap for injected CO2. Geologically, over time, some CO2 can react with rock minerals to form solid carbonates, further immobilizing the same.\|[0058] Additionally, a liquid carbon dioxide can be optionally mixed and/or adsorbed by the exhausted hydrocarbonaceous materials. Such materials can then be disposed in an appropriate manner. When referring to liquid carbon dioxide, the embodiments herein can also be used with supercritical carbon dioxide. As such, the discussion and embodiments presented herein referring to liquid carbon dioxide also can be applied with respect to supercritical carbon dioxide.\|[0059] In another embodiment, sequestering carbon dioxide can be achieved by injecting exhausted hydrocarbonaceous materials with the carbon dioxide. Such injection can provide adsorption of carbon dioxide. Additionally, such process can be performed with a catalyst or without a catalyst. Other metal and organic additives can be included as discussed herein. In one embodiment, such sequestering can include a metal selected from the group consisting of calcium, magnesium, including oxides thereof, silicates thereof, and mixtures thereof.\|[0060] With respect to carbon dioxide sequestering, a constructed permeability control infrastructure can comprise a permeability control impoundment defining a substantially encapsulated volume wherein the permeability control impoundment is substantially free of undisturbed geological formations, a comminuted hydrocarbonaceous material within the encapsulated volume forming a permeable body of hydrocarbonaceous material, and a carbon dioxide collection unit operatively connected to collect carbon dioxide from the control infrastructure. It is understood that the infrastructure can include any of the elements described herein including those elements that have been referred to in the context of a process. Additionally, the methods and processes described herein can include any elements described herein including those elements that have been referred to in the context of a composition or system.\|[0061] The carbon dioxide can be collected consistent with one or more of the above approaches using a corresponding carbon dioxide control unit. In one optional aspect, the carbon dioxide control unit can include a vessel for treatment and/or storage of the carbon dioxide. Additional storage tanks, pumps and/or vessels can also be used for transporting or storage of treatment chemicals and by-products. As described herein, the vessel can contain an aqueous solution, a metal, and carbon dioxide where the vessel is configured to react the carbon dioxide with the aqueous solution to form a precipitation of carbon dioxide with the metal. In another embodiment, the vessel can contain carbon dioxide where the vessel is configured to form liquid carbon dioxide from the carbon dioxide by cryogenic precipitation. Additionally, the vessel can contain exhausted hydrocarbonaceous materials that adsorb the liquid carbon dioxide. In one embodiment, the vessel can contain carbon dioxide where the vessel is configured to mix exhausted hydrocarbonaceous materials with the carbon dioxide such that the exhausted hydrocarbonaceous materials adsorb the carbon dioxide.\|[0062] In one embodiment, computer assisted mining, mine planning, hauling, blasting, assay, loading, transport, placement, and dust control measures can be utilized to fill and optimize the speed of mined material movement into the constructed capsule containment structure. In one alternative aspect, the impoundments can be formed in excavated volumes of a hydrocarbonaceous formation, although other locations remote from the control infrastructure can also be useful. For example, some hydrocarbonaceous formations have relatively thin hydrocarbon-rich layers, e.g. less than about 300 feet thick. Therefore, vertical mining and drilling tend to not be cost effective. In such cases, horizontal mining can be useful to recover the hydrocarbonaceous materials for formation of the permeable body. Although horizontal mining continues to be a challenging endeavor, a number of technologies have been developed and continue to be developed which can be useful in connection with the impoundments. In such cases, at least a portion of the impoundment can be formed across a horizontal layer, while other portions of the impoundment can be formed along and/or adjacent non-hydrocarbon bearing formation layers. Other mining approaches such as, but not limited to, room and pillar mining can provide an effective source of hydrocarbonaceous material with minimal waste and/or reclamation which can be transported to an impoundment and treated in accordance with the these principles.\|[0063] As mentioned herein, these systems and processes allow for a large degree of control regarding properties and characteristics of the permeable body which can be designed and optimized for a given installation. Impoundments, individually and across a plurality of impoundments can be readily tailored and classified based on varying composition of materials, intended products and the like. For example, several impoundments can be dedicated to production of heavy crude oil, while others can be configured for production of lighter products and/or syn gas. Non-limiting example of potential classifications and factors can include catalyst activity, enzymatic reaction for specific products, aromatic compounds, hydrogen content, microorganism strain or purpose, upgrading process, target final product, pressure (effects product quality and type), temperature, swelling behavior, aquathermal reactions, hydrogen donor agents, heat superdisposition, garbage impoundment, sewage impoundment, reusable pipes, and others. Typically, a plurality of these factors can be used to configure impoundments in a given project area for distinct products and purposes.\|[0064] The comminuted hydrocarbonaceous material can be filled into the control infrastructure to form the permeable body in any suitable manner. Typically the comminuted hydrocarbonaceous material can be conveyed into the control infrastructure by dumping, conveyors or other suitable approaches. As mentioned previously, the permeable body can have a suitably high void volume. Indiscriminate dumping can result in excessive compaction and reduction of void volumes. Thus, the permeable body can be formed by low compaction conveying of the hydrocarbonaceous material into the infrastructure. For example, retracting conveyors can be used to deliver the material near a top surface of the permeable body as it is formed. In this way, the hydrocarbonaceous material can retain a significant void volume between particles without substantial further crushing or compaction despite some small degree of compaction which often results from lithostatic pressure as the permeable body is formed.\|[0065] Once a desired permeable body has been formed within the control infrastructure, heat can be introduced sufficient to begin removal of hydrocarbons, e.g. via pyrolysis. A suitable heat source can be thermally associated with the permeable body. Optimal operating temperatures within the permeable body can vary depending on the composition and desired products. However, as a general guideline, operating temperatures can range from about 200° F. to about 750° F. Temperature variations throughout the encapsulated volume can vary and may reach as high as 900° F. or more in some areas. In one embodiment, the operating temperature can be a relatively lower temperature to facilitate production of liquid product such as from about 200° F. to about 650° F. This heating step can be a roasting operation which results in beneficiation of the crushed ore of the permeable body. Further, one embodiment comprises controlling the temperature, pressure and other variables sufficient to produce predominantly, and in some cases substantially only, liquid product. Generally, products can include both liquid and gaseous products, while liquid products can require fewer processing steps such as scrubbers etc. The relatively high permeability of the permeable body allows for production of liquid hydrocarbon products and minimization of gaseous products, depending to some extent on the particular starting materials and operating conditions. In one embodiment, the recovery of hydrocarbon products can occur substantially in the absence of cracking within the permeable body.\|[0066] In one aspect, heat can be transferred to the permeable body via convection. Heated gases can be injected into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body. Heated gases can be produced by combustion of natural gas, hydrocarbon product, or any other suitable source. Non-limiting examples of suitable heat transfer fluids can include hot air, hot exhaust gases, steam, hydrocarbon vapors and/or hot liquids. The heated gases can be imported from external sources or recovered from the process.\|[0067] Alternatively, or in combination with convective heating, a highly configurable approach can include embedding a plurality of conduits within the permeable body. The conduits can be configured for use as heating pipes, cooling pipes, heat transfer pipes, drainage pipes, or gas pipes. Further, the conduits can be dedicated to a single function or may serve multiple functions during operation of the infrastructure, i.e. heat transfer and drainage. The conduits can be formed of any suitable material, depending on the intended function. Non-limiting examples of suitable materials can include clay pipes, refractory cement pipes, refractory ECC pipes, poured in place pipes, metal pipes such as cast iron, stainless steel etc., polymer such as PVC, and the like. In one specific embodiment, all or at least a portion of the embedded conduits can comprise a degradable material. For example, non-galvanized 6″ cast iron pipes can be effectively used for single use embodiments and perform well over the useful life of the impoundment, typically less than about 2 years. Further, different portions of the plurality of conduits can be formed of different materials. Poured in place pipes can be especially useful for very large encapsulation volumes where pipe diameters exceed several feet. Such pipes can be formed using flexible wraps which retain a viscous fluid in an annular shape. For example, PVC pipes can be used as a portion of a form along with flexible wraps, where concrete or other viscous fluid is pumped into an annular space between the PVC and flexible wrap. Depending on the intended function, perforations or other apertures can be made in the conduits to allow fluids to flow between the conduits and the permeable body. Typical operating temperatures exceed the melting point of conventional polymer and resin pipes. In some embodiments, the conduits can be placed and oriented such that the conduits intentionally melt or otherwise degrade during operation of the infrastructure.\|[0068] The plurality of conduits can be readily oriented in any configuration, whether substantially horizontal, vertical, slanted, branched, or the like. At least a portion of the conduits can be oriented along predetermined pathways prior to embedding the conduits within the permeable body. The predetermined pathways can be designed to improve heat transfer, gas-liquid-solid contacting, maximize fluid delivery or removal from specific regions within the encapsulated volume, or the like. Further, at least a portion the conduits can be dedicated to heating of the permeable body. These heating conduits can be selectively perforated to allow heated gases or other fluids to convectively heat and mix throughout the permeable body. The perforations can be located and sized to optimize even and/or controlled heating throughout the permeable body. Alternatively, the heating conduits can form a closed loop such that heating gases or fluids are segregated from the permeable body. Thus, a “closed loop” does not necessarily require recirculation, rather isolation of heating fluid from the permeable body. In this manner, heating can be accomplished primarily or substantially only through thermal conduction across the conduit walls from the heating fluids into the permeable body. Heating in a closed loop allows for prevention of mass transfer between the heating fluid and permeable body and can reduce formation and/or extraction of gaseous hydrocarbon products.\|[0069] During the heating or roasting of the permeable body, localized areas of heat which exceed parent rock decomposition temperatures, often above about 900° F., can reduce yields and form carbon dioxide and undesirable contaminating compounds which can lead to leachates containing heavy metals, soluble organics and the like. The heating conduits can allow for substantial elimination of such localized hot spots while maintaining a vast majority of the permeable body within a desired temperature range. The degree of uniformity in temperature can be a balance of cost (e.g. for additional heating conduits) versus yields. However, at least about 85% of the permeable body can readily be maintained within about 5-10% of a target temperature range with substantially no hot spots, i.e. exceeding the decomposition temperature of the hydrocarbonaceous materials such as about 800° F. and in many cases about 900° F. Thus, operated as described herein, the systems can allow for recovery of hydrocarbons while eliminating or substantially avoiding production of undesirable leachates. Although products can vary considerably depending on the starting materials, high quality liquid and gaseous products are possible. In accordance with one embodiment, a crushed oil shale material can produce a liquid product having an API from about 30 to about 45, with about 33 to about 38 being currently typical, directly from the oil shale without additional treatment. Interestingly, practice of these processes has led to an understanding that pressure appears to be a much less influential factor on the quality of recovered hydrocarbons than temperature and heating times. Although heating times can vary considerably, depending on void space, permeable body composition, quality, etc., as a general guideline times can range from a few days (i.e. 3-4 days) up to about one year. In one specific example, heating times can range from about 2 weeks to about 4 months. Under-heating oil shale at short residence times, i.e. minutes to several hours, can lead to formation of leachable and/or somewhat volatile hydrocarbons. Accordingly, these systems and methods allow for extended residence times at moderate temperatures such that organics present in oil shale can be volatilized and/or carbonized, leaving insubstantial leachable organics. In addition, the underlying shale is not generally decomposed or altered which reduces soluble salt formation.\|[0070] Further, conduits can be oriented among a plurality of impoundments and/or control infrastructures to transfer fluids and/or heat between the structures. The conduits can be welded to one another using conventional welding or the like. Further, the conduits can include junctions which allow for rotation and or small amounts of movement during expansion and subsidence of material in the permeable body. Additionally, the conduits can include a support system which acts to support the assembly of conduits prior to and during filling of the encapsulated volume, as well as during operation. For example, during heating flows of fluids, heating and the like can cause expansion (fracturing or popcorn effect) or subsidence sufficient to create potentially damaging stress and strain on the conduits and associated junctions. A truss support system or other similar anchoring members can be useful in reducing damage to the conduits. The anchoring members can include cement blocks, 1-beams, rebar, columns, etc. which can be associated with walls of the impoundment, including side walls, floors and ceilings.\|[0071] Alternatively, the conduits can be completely constructed and assembled prior to introduction of any mined materials into the encapsulated volume. Care and planning can be considered in designing the predetermined pathways of the conduits and method of filling the volume in order to prevent damage to the conduits during the filling process as the conduits are buried. Thus, as a general rule, the conduits are oriented ab initio, or prior to embedding in the permeable body such that they are non-drilled. As a result, construction of the conduits and placement thereof can be performed without extensive core drilling and/or complicated machinery associated with well-bore or horizontal drilling. Rather, horizontal or any other orientation of conduit can be readily achieved by assembling the desired predetermined pathways prior to, or contemporaneous with, filling the infrastructure with the mined hydrocarbonaceous material. The non-drilled, hand/crane-placed conduits oriented in various geometric patterns can be laid with valve controlled connecting points which yield precise and closely monitored heating within the capsule impoundment. The ability to place and layer conduits including connecting, bypass and flow valves, and direct injection and exit points, allow for precision temperature and heating rates, precision pressure and pressurization rates, and precision fluid and gas ingress, egress and composition admixtures. For example, when a bacteria, enzyme, or other biological material is used, optimal temperatures can be readily maintained throughout the permeable body to increase performance, reaction, and reliability of such biomaterials.\|[0072] The conduits will generally pass through walls of the constructed infrastructure at various points. Due to temperature differences and tolerances, it can be beneficial to include an insulating material at the interface between the wall and the conduits. The dimensions of this interface can be minimized while also allowing space for thermal expansion differences during startup, steady-state operation, fluctuating operating conditions, and shutdown of the infrastructure. The interface can also involve insulating materials and sealant devices which prevent uncontrolled egress of hydrocarbons or other materials from the control infrastructure. Non-limiting examples of suitable materials can include high temperature gaskets, metal alloys, ceramics, clay or mineral liners, composites or other materials which having melting points above typical operating temperatures and act as a continuation of the permeability control provided by walls of the control infrastructure.\|[0073] Further, walls of the constructed infrastructure can be configured to minimize heat loss. In one aspect, the walls can be constructed having a substantially uniform thickness which is optimized to provide sufficient mechanical strength while also minimizing the volume of wall material through which the conduits pass. Specifically, excessively thick walls can reduce the amount of heat which is transferred into the permeable body by absorbing the same through conduction. Conversely, the walls can also act as a thermal barrier to somewhat insulate the permeable body and retain heat therein during operation.\|[0074] In one embodiment, fluid and gas compounds within the permeable body can be altered for desired extractive products using, as an example, induced pressure through gases or piled lithostatic pressure from piled rubble. Thus, some degree of upgrading and/or modification can be accomplished simultaneous with the recovery process. Further, certain hydro carbonaceous materials can require treatment using specific diluents or other materials. For example, treatment of tar sands can be readily accomplished by steam injection or solvent injection to facilitate separation of bitumen from sand particles according to well known mechanisms.\|[0075] With the above description in mind, FIG. 1 depicts a side view of one embodiment showing an engineered capsule containment and extraction impoundment 100 where existing grade 108 is used primarily as support for the impermeable floor layer 112. Exterior capsule impoundment side walls 102 provide containment and can, but need not be, subdivided by interior walls 104. Subdividing can create separate containment capsules 122 within a greater capsule containment of the impoundment 100 which can be any geometry, size or subdivision. Further subdivisions can be horizontally or vertically stacked. By creating separate containment capsules 122 or chambers, classification of lower grade materials, varied gases, varied liquids, varied process stages, varied enzymes or microbiology types, or other desired and staged processes can be readily accommodated. Sectioned capsules constructed as silos within larger constructed capsules can also be designed to provide staged and sequenced processing, temperatures, gas and fluid compositions and thermal transfers. Such sectioned capsules can provide additional environmental monitoring and can be built of lined and engineered tailings berms similar to the primary exterior walls. In one embodiment, sections within the impoundment 100 can be used to place materials in isolation, in the absence of external heat, or with the intent of limited or controlled combustion or solvent application. Lower content hydrocarbon bearing material can be useful as a combustion material or as fill or a berm wall building material. Material which does not meet a various cut-off grade thresholds can also be sequestered without alteration in an impoundment dedicated for such purpose. In such embodiments, such areas may be completely isolated or bypassed by heat, solvents, gases, liquids, or the like. Optional monitoring devices and/or equipment can be permanently or temporarily installed within the impoundment or outside perimeters of the impoundments in order to verify containment of the sequestered material.\|[0076] Walls 102 and 104 as well as cap 116 and impermeable layer 112 can be engineered and reinforced by gabions 146 and or geogrid 148 layered in fill compaction. Alternatively, these walls 102, 104, 116 and 112 which comprise the permeability control impoundment and collectively define the encapsulated volume can be formed of any other suitable material as previously described. In this embodiment, the impoundment 100 includes side walls 102 and 104 which are self-supporting. In one embodiment, tailings berms, walls, and floors can be compacted and engineered for structure as well as permeability. The use of compacted geogrids and other deadman structures for support of berms and embankments can be included prior to or incorporated with permeability control layers which may include sand, clay, bentonite clay, gravel, cement, grout, reinforced cement, refractory cements, insulations, geo-membranes, drainpipes, temperature resistant insulations of penetrating heated pipes, etc.\|[0077] In one alternative embodiment, the permeability control impoundment can include side walls which are compacted earth and/or undisturbed geological formations while the cap and floors are impermeable. Specifically, in such embodiments an impermeable cap can be used to prevent uncontrolled escape of volatiles and gases from the impoundment such that appropriate gas collection outlets can be used. Similarly, an impermeable floor can be used to contain and direct collected liquids to a suitable outlet such the drain system 133 to remove liquid products from lower regions of the impoundment. Although impermeable side walls can be desirable in some embodiments, such are not always required. In some cases, side walls can be exposed undisturbed earth or compacted fill or earth, or other permeable material. Having permeable side walls may allow some small egress of gases and/or liquids from the impoundment.\|[0078] Although not shown, above, below, around and adjacent to constructed capsule containment vessels environmental hydrology measures can be engineered to redirect surface water away from the capsule walls, floors, caps, etc. during operation. Further, gravity assisted drainage pipes and mechanisms can be utilized to aggregate and channel fluids, liquids or solvents within the encapsulated volume to central gathering, pumping, condensing, heating, staging and discharge pipes, silos, tanks, and/or wells as needed. In a similar manner, steam and/or water which is intentionally introduce, e.g. for tar sands bitumen treatment, can be recycled.\|[0079] Once wall structures 102 and 104 have been constructed above a constructed and impermeable floor layer 112 which commences from ground surface 106, the mined rubble 120 (which may be crushed or classified according to size or hydrocarbon richness), can be placed in layers upon (or next to) placed tubular heating pipes 118, fluid drainage pipes 124, and, or gas gathering or injection pipes 126. These pipes can be oriented and designed in any optimal flow pattern, angle, length, size, volume, intersection, grid, wall sizing, alloy construction, perforation design, injection rate, and extraction rate. In some cases, pipes such as those used for heat transfer can be connected to, recycled through or derive heat from heat source 134. Alternatively, or in combination with, recovered gases can be condensed by a condenser 140. Heat recovered by the condenser can be optionally used to supplement heating of the permeable body or for other process needs.\|[0080] Heat source 134 can derive, amplify, gather, create, combine, separate, transmit or include heat derived from any suitable heat source including, but not limited to, fuel cells (e.g. solid oxide fuel cells, molten carbonate fuel cells and the like), solar sources, wind sources, hydrocarbon liquid or gas combustion heaters, geothermal heat sources, nuclear power plant, coal fired power plant, radio frequency generated heat, wave energy, flameless combustors, natural distributed combustors, or any combination thereof. In some cases, electrical resistive heaters or other heaters can be used, although fuel cells and combustion-based heaters are particularly effective. In some locations, geothermal water can be circulated to the surface in adequate amounts to heat the permeable body and directed into the infrastructure.\|[0081] In another embodiment, electrically conductive material can be distributed throughout the permeable body and an electric current can be passed through the conductive material sufficient to generate heat. The electrically conductive material can include, but is not limited to, metal pieces or beads, conductive cement, metal coated particles, metal-ceramic composites, conductive semi-metal carbides, calcined petroleum coke, laid wire, combinations of these materials, and the like. The electrically conductive material can be premixed having various mesh sizes or the materials can be introduced into the permeable body subsequent to formation of the permeable body.\|[0082] Liquids or gases can transfer heat from heat source 134, or in another embodiment, in the cases of hydrocarbon liquid or gas combustion, radio frequency generators (microwaves), or fuel cells all can, but need not, actually generate heat inside of capsule impoundment area 114 or 122. In one embodiment, heating of the permeable body can be accomplished by convective heating from hydrocarbon combustion. Of particular interest is hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen. Stoichiometric conditions can allow for significantly increased heat gas temperatures. Stoichiometric combustion can employ but does not generally require a pure oxygen source which can be provided by known technologies including, but not limited to, oxygen concentrators, membranes, electrolysis, and the like. In some embodiments oxygen can be provided from air with stoichiometric amounts of oxygen and hydrogen. Combustion off gas can be directed to an ultra-high temperature heat exchanger, e.g. a ceramic or other suitable material having an operating temperature above about 2500° F. Air obtained from ambient or recycled from other processes can be heated via the ultra high temperature heat exchanger and then sent to the impoundment for heating of the permeable body. The combustion off gases can then be sequestered without the need for further separation, i.e. because the off gas is predominantly carbon dioxide and water.\|[0083] In order to minimize heat losses, distances can be minimized between the combustion chamber, heat exchanger, and impoundments. Therefore, in one specific detailed embodiment portable combustors can be attached to individual heating conduits or smaller sections of conduits. Portable combustors or burners can individually provide from about 100,000 Btu to about 1,000,000 Btu with about 600,000 Btu per pipe generally being sufficient.\|[0084] Alternatively, in-capsule combustion can be initiated inside of isolated capsules within a primary constructed capsule containment structure. This process partially combusts hydrocarbonaceous material to provide heat and intrinsic pyrolysis. Unwanted air emissions 144 can be captured and sequestered in a formation 108 once derived from capsule containment 114, 122 or from heat source 134 and delivered by a drilled well bore 142. Heat source 134 can also create electricity and transmit, transform or power via electrical transmission lines 150. The liquids or gases extracted from capsule impoundment treatment area 114 or 122 can be stored in a nearby holding tank 136 or within a capsule containment 114 or 122. For example, the impermeable floor layer 112 can include a sloped area 110 which directs liquids towards drain system 133 where liquids are directed to the holding tank.\|[0085] As rubble material 120 is placed with piping 118, 124, 126, and 128, various measurement devices or sensors 130 are envisioned to monitor temperature, pressure, fluids, gases, compositions, heating rates, density, and all other process attributes during the extractive process within, around, or underneath the engineered capsule containment impoundment 100. Such monitoring devices and sensors 130 can be distributed anywhere within, around, part of, connected to, or on top of placed piping 118, 124, 126, and 128 or, on top of, covered by, or buried within rubble material 120 or impermeable barrier zone 112.\|[0086] As placed rubble material 120 fills the capsule treatment area 114 or 122, 120 becomes the ceiling support for engineered impermeable cap barrier zone 138, and wall barrier construction 170, which may include any combination of impermeability and engineered fluid and gas barrier or constructed capsule construction comprising those which may make up 112 including, but not limited to clay 162, compacted fill or import material 164, cement or refractory cement containing material 166, geo synthetic membrane, liner or insulation 168. Above 138, fill material which can be oriented as ceiling cap 116 is placed to create lithostatic pressure upon the capsule treatment areas 114 or 122. Covering the permeable body with compacted fill sufficient to create an increased lithostatic pressure within the permeable body can be useful in further increasing hydrocarbon product quality. A compacted fill ceiling can substantially cover the permeable body, while the permeable body in return can substantially support the compacted fill ceiling. The compacted fill ceiling can further be sufficiently impermeable to removed hydrocarbon or an additional layer of permeability control material can be added in a similar manner as side and/or floor walls. Additional pressure can be introduced into extraction capsule treatment area 114 or 122 by increasing any gas or fluid once extracted, treated or recycled, as the case may be, via any of piping 118, 124, 126, or 128. All relative measurements, optimization rates, injection rates, extraction rates, temperatures, heating rates, flow rates, pressure rates, capacity indicators, chemical compositions, or other data relative to the process of heating, extraction, stabilization, sequestration, impoundment, upgrading, refining or structure analysis within the capsule impoundment 100 are envisioned through connection to a computing device 132 which operates computer software for the management, calculation and optimization of the entire process. Further, core drilling, geological reserve analysis and assay modeling of a formation prior to blasting, mining and hauling (or at any time before, after or during such tasks) can serve as data input feeds into computer controlled mechanisms that operate software to identify optimal placements, dimensions, volumes and designs calibrated and cross referenced to desired production rate, pressure, temperature, heat input rates, gas weight percentages, gas injection compositions, heat capacity, permeability, porosity, chemical and mineral composition, compaction, density. Such analysis and determinations may include other factors like weather data factors such as temperature and air moisture content impacting the overall performance of the constructed infrastructure. Other data such as ore moisture content, hydrocarbon richness, weight, mesh size, and mineral and geological composition can be utilized as inputs including time value of money data sets yielding project cash flows, debt service, and internal rates of return.\|[0087] FIG. 2A shows a collection of impoundments including an uncovered or uncapped capsule impoundment 100, containing sectioned capsule impoundments 122 inside of a mining quarry 200 with various elevations of bench mining. FIG. 2B illustrates a single impoundment 122 without associated conduits and other aspects merely for clarity. This impoundment can be similar to that illustrated in FIG. 1 or any other configuration. In some embodiments, it is envisioned that mining rubble can be transferred down chutes 230 or via conveyors 232 to the quarry capsule impoundments 100 and 122 without any need of mining haul trucks.\|[0088] FIG. 3 shows the engineered permeability barriers 112 below capsule impoundment 100 resting on existing grade 106 of formation 108 with cap covering material or fill 302 on the sides and top of capsule impoundment 100 to ultimately (following the process) cover and reclaim a new earth surface 300. Indigenous plants which may have been temporarily moved from the area may be replanted such as trees 306. The constructed infrastructures can generally be single use structures which can be readily and securely shut down with minimal additional remediation. This can dramatically reduce costs associated with moving large volumes of spent materials. However, in some circumstances the constructed infrastructures can be excavated and reused. Some equipment such as radio frequency (RF) mechanisms, tubulars, devices, and emitters may be recovered from within the constructed impoundment upon completion of hydrocarbon recovery.\|[0089] FIG. 4 shows computer means 130 controlling various property inputs and outputs of conduits 118, 126, or 128 connected to heat source 134 during the process among the subdivided impoundments 122 within a collective impoundment 100 to control heating of the permeable body. Similarly, liquid and vapor collected from the impoundments can be monitored and collected in tank 136 and condenser 140, respectively. Condensed liquids from the condenser can be collected in tank 141, while non-condensable vapor collected at unit 143. As described previously, the liquid and vapor products can be combined or more often left as separate products depending on condensability, target product, and the like. A portion of the vapor product can be optionally condensed and combined with the liquid products in tank 136. However, much of the vapor product will be C4 and lighter gases which can be burned, sold, or used within the process. For example, hydrogen gas may be recovered using conventional gas separation and used to hydrotreat the liquid products according to conventional upgrading methods, e.g. catalytic, etc. or the non-condensable gaseous product can be burned to produce heat for use in heating the permeable body, heating an adjacent or nearby impoundment, heating service or personnel areas, or satisfying other process heat requirements. The constructed infrastructure can include thermocouples, pressure meters, flow meters, fluid dispersion sensors, richness sensors and any other conventional process control devices distributed throughout the constructed infrastructure. These devices can be each operatively associated with a computer such that heating rates, product flow rates, and pressures can be monitored or altered during heating of the permeable body. Optionally, in-place agitation can be performed using, for example, ultrasonic generators which are associated with the permeable body. Such agitation can facilitate separation and pyrolysis of hydrocarbons from the underlying solid materials with which they are associated. Further, sufficient agitation can reduce clogging and agglomeration throughout the permeable body and the conduits.\|[0090] FIG. 5 shows how any of the conduits can be used to transfer heat in any form of gas, liquid or heat via transfer means 510 from any sectioned capsule impoundment to another. Then, cooled fluid can be conveyed via heat transfer means 512 to the heat originating capsule 500, or heat originating source 134 to pick up more heat from capsule 500 to be again recirculated to a destination capsule 522. Thus, various conduits can be used to transfer heat from one impoundment to another in order to recycle heat and manage energy usage to minimize energy losses.\|[0091] In yet another aspect, a hydrogen donor agent can be introduced into the permeable body during the step of heating. The hydrogen donor agent can be any composition which is capable of hydrogenation of the hydrocarbons and can optionally be a reducing agent. Non-limiting examples of suitable hydrogen donor agents can include synthesis gas, propane, methane, hydrogen, natural gas, natural gas condensate, industrial solvents such as acetones, toluenes, benzenes, xylenes, cumenes, cyclopentanes, cyclohexanes, lower alkenes (C4-C10), terpenes, substituted compounds of these solvents, etc., and the like. Further, the recovered hydrocarbons can be subjected to hydrotreating either within the permeable body or subsequent to collection. Advantageously, hydrogen recovered from the gas products can be reintroduced into the liquid product for upgrading. Regardless, hydrotreating or hydrodesulfurization can be very useful in reducing nitrogen and sulfur content in final hydrocarbon products. Optionally, catalysts can be introduced to facilitate such reactions. In addition, introduction of light hydrocarbons into the permeable body can result in reforming reactions which reduce the molecular weight, while increasing the hydrogen to carbon ratio. This is particularly advantageous due at least in part to high permeability of the permeable body, e.g. often around 30%-40% void volume although void volume can generally vary from about 10% to about 50% void volume. Light hydrocarbons which can be injected can be any which provide reforming to recovered hydrocarbons. Non-limiting examples of suitable light hydrocarbons include natural gas, natural gas condensates, industrial solvents, hydrogen donor agents, and other hydrocarbons having ten or fewer carbons, and often five or fewer carbons. Currently, natural gas is an effective, convenient, and plentiful light hydrocarbon. As mentioned previously, various solvents or other additives can also be added to aid in extraction of hydrocarbon products from the oil shale and can often also increase fluidity.\|[0092] The light hydrocarbon can be introduced into the permeable body by conveying the same through a delivery conduit having an open end in fluid communication with a lower portion of the permeable body such that the light hydrocarbons (which are a gas under normal operating conditions) permeate up through the permeable body. Alternatively, this same approach can be applied to recovered hydrocarbons which are first delivered to an empty impoundment. In this way, the impoundment can act as a holding tank for direct products from a nearby impoundment and as a reformer or upgrader. In this embodiment, the impoundment can be at least partially filled with a liquid product where the gaseous light hydrocarbon is passed through and allowed to contact the liquid hydrocarbon products at temperatures and conditions sufficient to achieve reforming in accordance with well known processes. Optional reforming catalysts which include metals such as Pd, Ni or other suitable catalytically active metals can also be included in the liquid product within the impoundment. The addition of catalysts can serve to lower and/or adjust reforming temperature and/or pressure for particular liquid products. Further, the impoundments can be readily formed at almost any depth. Thus, optimal reforming pressures (or recovery pressures when using impoundment depth as pressure control measure for recovery from a permeable body) can be designed based on hydrostatic pressure due to the amount of liquid in the impoundment and the height of the impoundment, i.e. P=ρgh. In addition, the pressure can vary considerably over the height of the impoundment sufficient to provide multiple reforming zones and tailorable pressures. Generally, pressures within the permeable body can be sufficient to achieve substantially only liquid extraction, although some minor volumes of vapor may be produced depending on the particular composition of the permeable body. As a general guideline, pressures can range from about 5 atm to about 50 atm, although pressures from about 6 atm to about 20 atm can be particularly useful. However, any pressure greater than about atmospheric can be used.\|[0093] In one embodiment, extracted crude has fines precipitated out within the subdivided capsules. Extracted fluids and gases can be treated for the removal of fines and dust particles. Separation of fines from shale oil can be accomplished by techniques such as, but not limited to, hot gas filtering, precipitation, and heavy oil recycling.\|[0094] Hydrocarbon products recovered from the permeable body can be further processed (e.g. refined) or used as produced. Any condensable gaseous products can be condensed by cooling and collection, while non-condensable gases can be collected, burned as fuel, reinjected, or otherwise utilized or disposed of. Optionally, mobile equipment can be used to collect gases. These units can be readily oriented proximate to the control infrastructure and the gaseous product directed thereto via suitable conduits from an upper region of the control infrastructure.\|[0095] In yet another alternative embodiment, heat within the permeable body can be recovered subsequent to primary recovery of hydrocarbon materials therefrom. For example, a large amount of heat is retained in the permeable body. In one optional embodiment, the permeable body can be flooded with a heat transfer fluid such as water to form a heated fluid, e.g. heated water and/or steam. At the same time, this process can facilitate removal of some residual hydrocarbon products via a physical rinsing of the spent shale solids. In some cases, the introduction of water and presence of steam can result in water gas shift reactions and formation of synthesis gas. Steam recovered from this process can be used to drive a generator, directed to another nearby infrastructure, or otherwise used. Hydrocarbons and/or synthesis gas can be separated from the steam or heated fluid by conventional methods.\|[0096] Although the methods and infrastructure allow for improved permeability and control of operating conditions, significant quantities of unrecovered hydrocarbons, precious metals, minerals, sodium bicarbonate or other commercially valuable materials often remain in the permeable body. Therefore, a selective solvent can be injected or introduced into the permeable body. Typically, this can be done subsequent to collecting the hydrocarbons, although certain selective solvents can be beneficially used prior to heating and/or collection. This can be done using one or more of the existing conduits or by direct injection and percolation through the permeable body. The selective solvent or leachate can be chosen as a solvent for one or more target materials, e.g. minerals, precious metal, heavy metals, hydrocarbons, or sodium bicarbonate. In one specific embodiment, steam or carbon dioxide can be used as a rinse of the permeable body to dislodge at least a portion of any remaining hydrocarbons. This can be beneficial not only in removing potentially valuable secondary products, but also in cleaning remaining spent materials of trace heavy metal or inorganics to below detectable levels in order to comply with regulatory standards or to prevent inadvertent leaching of materials at a future date.\|[0097] More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body. Typically, such recovery of materials can be performed prior to heat treatment of the permeable body. Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like. For example, heavy metals, bauxite or aluminum, and mercury can be removed by flooding the permeable body with an appropriate solvent and recirculating the resulting leachate through appropriately designed ion exchange resins (e.g. beads, membranes, etc.).\|[0098] Similarly, bioextraction, bioleaching, biorecovery, or bioremediation of hydrocarbon material, spent materials, or precious metals can be performed to further improve remediation, extract valuable metals, and restoration of spent material to environmentally acceptable standards. In such bioextraction scenarios, conduits can be used to inject catalyzing gases as a precursor which helps to encourage bioreaction and growth. Such microorganisms and enzymes can biochemically oxidize the ore body or material or cellulosic or other biomass material prior to an ore solvent extraction via bio-oxidation. For example, a perforated pipe or other mechanism can be used to inject a light hydrocarbon (e.g. methane, ethane, propane or butane) into the permeable body sufficient to stimulate growth and action of native bacteria. Bacteria can be native or introduced and may grow under aerobic or anaerobic conditions. Such bacteria can release metals from the permeable body which can then be recovered via flushing with a suitable solvent or other suitable recovery methods. The recovered metals can then be precipitated out using conventional methods.\|[0099] Synthesis gas can also be recovered from the permeable body during the step of heating. Various stages of gas production can be manipulated through processes which raise or lower operating temperatures within the encapsulated volume and adjust other inputs into the impoundment to produce synthetic gases which can include but are not limited to, carbon monoxide, hydrogen, hydrogen sulfide, hydrocarbons, ammonia, water, nitrogen or various combinations thereof. In one embodiment, temperature and pressure can be controlled within the permeable body to lower CO2 emissions as synthetic gases are extracted.\|[0100] Hydrocarbon product recovered from the constructed infrastructures can most often be further processed, e.g. by upgrading, refining, etc. Sulfur from related upgrading and refining processing can be isolated in various constructed sulfur capsules within the greater structured impoundment capsule. Constructed sulfur capsules can be spent constructed infrastructures or dedicated for the purpose of storage and isolation after desulfurization.\|[0101] Similarly, spent hydrocarbonaceous material remaining in the constructed infrastructure can be utilized in the production of cement and aggregate products for use in construction or stabilization of the infrastructure itself or in the formation of offsite constructed infrastructures. Such cement products made with the spent shale may include, but are not limited to, mixtures with Portland cement, calcium salt, volcanic ash, perlite, synthetic nano carbons, sand, fiber glass, crushed glass, asphalt, tar, binding resins, cellulosic plant fibers, and the like.\|[0102] In still another embodiment, injection, monitoring and production conduits or extraction egresses can be incorporated into any pattern or placement within the constructed infrastructure. Monitoring wells and constructed geo membrane layers beneath or outside of the constructed capsule containment can be employed to monitor unwanted fluid and moisture migration outside of containment boundaries and the constructed infrastructure.\|[0103] Although a filled and prepared constructed infrastructure can often be immediately heated to recover hydrocarbons, this is not required. For example, a constructed infrastructure which is built and filled with mined hydrocarbonaceous material can be left in place as a proven reserve. Such structures are less susceptible to explosion or damage due to terrorist activity and can also provide strategic reserves of unprocessed petroleum products, with classified and known properties so that economic valuations can be increased and more predictable. Long term petroleum storage often faces quality deterioration issues over time. Thus, these approaches can optionally be used for long term quality insurance and storage with reduced concerns regarding breakdown and degradation of hydrocarbon products.\|[0104] In still another aspect, the high quality liquid product can be blended with more viscous lower quality (e.g. lower API) hydrocarbon products. For example, kerogen oil produced from the impoundments can be blended with bitumen to form a blended oil. The bitumen is typically not transportable through an extended pipeline under conventional and accepted pipeline standards and can have a viscosity substantially above and an API substantially below that of the kerogen oil. By blending the kerogen oil and bitumen, the blended oil can be rendered transportable without the use of additional diluents or other viscosity or API modifiers. As a result, the blended oil can be pumped through a pipeline without requiring additional treatments to remove a diluent or returning such diluents via a secondary pipeline. Conventionally, bitumen is combined with a diluent such as natural gas condensate or other low molecular weight liquids, to allow pumping to a remote location. The diluent is removed and returned via a second pipeline back to the bitumen source. These approaches allow for elimination of returning diluent and simultaneous upgrading of the bitumen.\|[0105] Difficult problems can thus be solved related to the extraction of hydrocarbon liquids and gases from surface or underground mined hydrocarbon bearing deposits such as oil shale, tar sands, lignite, and coal, and from harvested biomass. Among other things, these methods and systems help reduce cost, increase volume output, lower air emissions, limit water consumption, prevent underground aquifer contamination, reclaim surface disturbances, reduce material handling costs, remove dirty fine particulates, and improve composition of recovered hydrocarbon liquid or gas. Water contamination issues can also be addressed with a safer, more predictable, engineered, observable, repairable, adaptable and preventable water protection structure.\|[0106] Although the described methods and systems are mining-dependent, they are not limited or encumbered to conventional aboveground (ex-situ) retorting processes. This approach improves upon the benefits of surface retorts including better process control of temperature, pressure, injection rates, fluid and gas compositions, product quality and better permeability due to processing and heating mined rubble. These advantages are available while still addressing the volume, handling, and scalability issues most fabricated surface retorts cannot provide.\|[0107] Other improvements which can be realized are related to environmental protection. Conventional surface retorts have had the problem of spent shale after it has been mined and has passed through a surface retort. Spent shale which has been thermally altered requires special handling to reclaim and isolate from surface drainage basins and underground aquifers. These methods and systems can address reclamation and retorting in a uniquely combined approach. In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants.\|[0108] It is to be understood that the above-referenced arrangements are illustrative of the application for the principles of the present invention. Thus, while the present invention has been described above in connection with the exemplary embodiments, it will be apparent to those of ordinary skill in the art that numerous modifications and alternative arrangements can be made without departing from the principles and concepts of the invention as set forth in the claims.	(US8323481)\|RELATED APPLICATION\|[0001] This application claims priority to U.S. Provisional Patent Application No. 61/152,220 filed Feb. 12, 2009 which is incorporated herein by reference.\|(US8323481)\|BACKGROUND\|[0002] Global and domestic demand for fossil fuels continues to rise despite price increases and other economic and geopolitical concerns. As such demand continues to rise, research and investigation into finding additional economically viable sources of fossil fuels correspondingly increases. Historically, many have recognized the vast quantities of energy stored in oil shale, coal and tar sand deposits, for example. However, these sources remain a difficult challenge in terms of economically competitive recovery. Canadian tar sands have shown that such efforts can be fruitful, although many challenges still remain, including environmental impact, product quality, production costs and process time, among others.\|[0003] Estimates of world-wide oil shale reserves range from two to almost seven trillion barrels of oil, depending on the estimating source. Regardless, these reserves represent a tremendous volume and remain a substantially untapped resource. A large number of companies and investigators continue to study and test methods of recovering oil from such reserves. In the oil shale industry, methods of extraction have included underground rubble chimneys created by explosions, in-situ methods such as In-Situ Conversion Process (ICP) method (Shell Oil), and heating within steel fabricated retorts. Other methods have included in-situ radio frequency methods (microwaves), and “modified” in-situ processes wherein underground mining, blasting and retorting have been combined to make rubble out of a formation to allow for better heat transfer and product removal.\|[0004] Among typical oil shale processes, all face tradeoffs in economics and environmental concerns. No current process alone satisfies economic, environmental, and technical challenges. Moreover, global warming concerns give rise to additional measures to address carbon dioxide (CO2) emissions which are associated with such processes. Methods are needed that accomplish environmental stewardship, yet still provide high-volume cost-effective oil production.\|[0005] Below ground in-situ concepts emerged based on their ability to produce high volumes while avoiding the cost of mining. While the cost savings resulting from avoiding mining can be achieved, the in-situ method requires heating a formation for a longer period of time due to the extremely low thermal conductivity and high specific heat of solid oil shale. Perhaps the most significant challenge for any in-situ process is the uncertainty and long term potential of water contamination that can occur with underground freshwater aquifers. In the case of Shell's ICP method, a “freeze wall” is used as a barrier to keep separation between aquifers and an underground treatment area. Although this is possible, no long term analysis has proven for extended periods to guarantee the prevention of contamination. Without guarantees and with even fewer remedies should a freeze wall fail, other methods are desirable to address such environmental risks.\|[0006] For this and other reasons, the need remains for methods and systems which can provide improved recovery of hydrocarbons from suitable hydrocarbon-containing materials, which have acceptable economics and avoid the drawbacks mentioned above.\|SUMMARY\|[0007] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating the hydrocarbonaceous material can be substantially stationary. Additionally, during heating, any carbon dioxide that is produced can be sequestered. Removed hydrocarbons can be collected for further processing, use in the process as supplemental fuel or additives, and/or direct use without further treatment.\|[0008] Additional features and advantages of these principles will be apparent from the following detailed description, which illustrates, by way of example, features of the invention.\|(US8323481)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0009] FIG. 1 is side partial cutaway view schematic of a constructed permeability control infrastructure in accordance with one embodiment.\|[0010] FIGS. 2A and 2B are top and plan views of a plurality of permeability control impoundments in accordance with one embodiment.\|[0011] FIG. 3 is a side cutaway view of a permeability control impoundment in accordance with one embodiment.\|[0012] FIG. 4 is a schematic of a portion of a constructed infrastructure in accordance with an embodiment.\|[0013] FIG. 5 is a schematic showing heat transfer between two permeability control impoundments in accordance with another embodiment.\|(US8323481)\|DETAILED DESCRIPTION\|[0014] It should be noted that the figures are merely exemplary of several embodiments and no limitations on the scope of the present invention are intended thereby. Further, the figures are generally not drawn to scale, but are drafted for purposes of convenience and clarity in illustrating various aspects of the invention.\|DETAILED DESCRIPTION\|[0015] Reference will now be made to exemplary embodiments and specific language will be used herein to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended. Alterations and further modifications of the inventive features described herein, and additional applications of the principles of the invention as described herein, which would occur to one skilled in the relevant art and having possession of this disclosure, are to be considered within the scope of the invention. Further, before particular embodiments are disclosed and described, it is to be understood that this invention is not limited to the particular process and materials disclosed herein as such may vary to some degree. It is also to be understood that the terminology used herein is used for the purpose of describing particular embodiments only and is not intended to be limiting, as the scope of the present invention will be defined only by the appended claims and equivalents thereof.\|DEFINITIONS\|[0016] In describing and claiming the present invention, the following terminology will be used.\|[0017] The singular forms “a,” “an,” and “the” include plural references unless the context clearly dictates otherwise. Thus, for example, reference to “a wall” includes reference to one or more of such structures, “a permeable body” includes reference to one or more of such materials, and “a heating step” refers to one or more of such steps.\|[0018] As used herein “existing grade” or similar terminology refers to the grade or a plane parallel to the local surface topography of a site containing an infrastructure as described herein which infrastructure may be above or below the existing grade.\|[0019] As used herein, “conduits” refers to any passageway along a specified distance which can be used to transport materials and/or heat from one point to another point. Although conduits can generally be circular pipes, other non-circular conduits can also be useful. Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|[0020] As used herein, “constructed infrastructure” refers to a structure which is substantially entirely man made, as opposed to freeze walls, sulfur walls, or other barriers which are formed by modification or filling pores of an existing geological formation.\|[0021] The constructed permeability control infrastructure is often substantially free of undisturbed geological formations, although the infrastructure can be formed adjacent or in direct contact with an undisturbed formation. Such a control infrastructure can be unattached or affixed to an undisturbed formation by mechanical means, chemical means, or a combination of such means, e.g. bolted into the formation using anchors, ties, or other suitable hardware.\|[0022] As used herein, “comminuted” refers to breaking a formation or larger mass into pieces. A comminuted mass can be rubbilized or otherwise broken into fragments.\|[0023] As used herein, “hydrocarbonaceous material” refers to any hydrocarbon-containing material from which hydrocarbon products can be extracted or derived. For example, hydrocarbons may be extracted directly as a liquid, removed via solvent extraction, directly vaporized or otherwise removed from the material. However, many hydro carbonaceous materials contain kerogen or bitumen which is converted to a hydrocarbon through heating and pyrolysis. Hydrocarbonaceous materials can include, but is not limited to, oil shale, tar sands, coal, lignite, bitumen, peat, and other organic materials.\|[0024] As used herein, “impoundment” refers to a structure designed to hold or retain an accumulation of fluid and/or solid moveable materials. An impoundment generally derives at least a substantial portion of foundation and structural support from earthen materials. Thus, the control walls do not always have independent strength or structural integrity apart from the earthen material and/or formation against which they are formed.\|[0025] As used herein, “permeable body” refers to any mass of comminuted hydro carbonaceous material having a relatively high permeability which exceeds permeability of a solid undisturbed formation of the same composition. Suitable permeable bodies can have greater than about 10% void space and typically have void space from about 30% to 45%, although other ranges may be suitable. Allowing for high permeability facilitates, for example, through the incorporation of large irregularly shaped particles, heating of the body through convection as the primary heat transfer while also substantially reducing costs associated with crushing to very small sizes, e.g. below about 1 to about 0.5 inch.\|[0026] As used herein, “wall” refers to any constructed feature having a permeability control contribution to confining material within an encapsulated volume defined at least in part by control walls. Walls can be oriented in any manner such as vertical, although ceilings, floors, and other contours defining the encapsulated volume can also be “walls” as used herein.\|[0027] As used herein, “mined” refers to a material which has been removed or disturbed from an original stratographic or geological location to a second and different location or returned to the same location. Typically, mined material can be produced by rubbilizing, crushing, explosively detonating, or otherwise removing material from a geologic formation.\|[0028] As used herein, “adsorb,” “adsorbing,” or “adsorbed” refers to the process where a gas or liquid solute accumulates on the surface of a solid or a liquid or diffuses into a solid or liquid. Generally, when referring to carbon dioxide, the carbon dioxide is adsorbed into a material such that the carbon dioxide is substantially immobilized.\|[0029] As used herein, “substantially stationary” refers to nearly stationary positioning of materials with a degree of allowance for subsidence, expansion, and/or settling as hydrocarbons are removed from the hydrocarbonaceous material from within the enclosed volume to leave behind lean material. In contrast, any circulation and/or flow of hydrocarbonaceous material such as that found in fluidized beds or rotating retorts involves highly substantial movement and handling of hydrocarbonaceous material.\|[0030] As used herein, “substantial” when used in reference to a quantity or amount of a material, or a specific characteristic thereof, refers to an amount that is sufficient to provide an effect that the material or characteristic was intended to provide. The exact degree of deviation allowable may in some cases depend on the specific context. Similarly, “substantially free of” or the like refers to the lack of an identified element or agent in a composition. Particularly, elements that are identified as being “substantially free of” are either completely absent from the composition, or are included only in amounts which are small enough so as to have no measurable effect on the composition.\|[0031] As used herein, “about” refers to a degree of deviation based on experimental error typical for the particular property identified. The latitude provided the term “about” will depend on the specific context and particular property and can be readily discerned by those skilled in the art. The term “about” is not intended to either expand or limit the degree of equivalents which may otherwise be afforded a particular value. Further, unless otherwise stated, the term “about” shall expressly include “exactly,” consistent with the discussion below regarding ranges and numerical data.\|[0032] Concentrations, dimensions, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of about 1 to about 200 should be interpreted to include not only the explicitly recited limits of 1 and 200, but also to include individual sizes such as 2, 3, 4, and sub-ranges such as 10 to 50, 20 to 100, etc.\|[0033] As used herein, a plurality of items, structural elements, compositional elements, and/or materials may be presented in a common list for convenience. However, these lists should be construed as though each member of the list is individually identified as a separate and unique member. Thus, no individual member of such list should be construed as a de facto equivalent of any other member of the same list solely based on their presentation in a common group without indications to the contrary.\|[0034] Carbon Management and Sequestration from Control Infrastructures\|[0035] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined or harvested hydro carbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure is a fixed structure. Additionally, during heating, at least a portion of carbon dioxide that is produced can be sequestered. Removed fluid hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.\|[0036] The constructed permeability control infrastructure can be formed using existing grade as floor support and/or as side wall support for the constructed infrastructure. For example, the control infrastructure can be formed as a free standing structure, i.e. using only existing grade as a floor with side walls being man-made. Alternatively, the control infrastructure can be formed within an excavated pit. Regardless, the control infrastructures are always formed above-grade.\|[0037] A constructed permeability control infrastructure can include a permeability control impoundment which defines a substantially encapsulated volume. The permeability control impoundment is substantially free of undisturbed geological formations. Specifically, the permeability control aspect of the impoundment can be completely constructed and manmade as a separate isolation mechanism for prevention of uncontrolled migration of material into or out of the encapsulated volume.\|[0038] In one embodiment, the permeability control impoundment can be formed along walls of an excavated hydrocarbonaceous material deposit. For example, oil shale, tar sands, or coal can be mined from a deposit to form a cavity which corresponds approximately to a desired encapsulation volume for an impoundment. The excavated cavity can then be used as a form and support to create the permeability control impoundment.\|[0039] In one alternative aspect, at least one additional excavated hydrocarbonaceous material deposit can be formed such that a plurality of impoundments can be operated. Further, such a configuration can facilitate a reduction in transportation distance of the mined material. Specifically, the mined hydro carbonaceous material for any particular encapsulated volume can be mined from an adjacent excavated hydrocarbonaceous material deposit. In this manner, a grid of constructed structures can be built such that mined material can be immediately and directly filled into an adjacent impoundment.\|[0040] Mining and/or excavation of hydrocarbonaceous deposits can be accomplished using any suitable technique. Conventional surface mining can be used, although alternative excavators can also be used without requirement of transportation of the mined materials. In one specific embodiment, the hydrocarbonaceous deposit can be excavated using a crane-suspended excavator. One example of a suitable excavator can include vertical tunnel boring machines. Such machines can be configured to excavate rock and material beneath the excavator. As material is removed, the excavator is lowered to ensure substantially continuous contact with a formation. Removed material can be conveyed out of the excavation area using conveyors or lifts. Alternatively, the excavation can occur under aqueous slurry conditions to reduce dust problems and act as a lubricant/coolant. The slurry material can be pumped out of the excavation for separation of solids in a settling tank or other similar solid-liquid separator, or the solids may be allowed to precipitate directly in an impoundment. This approach can be readily integrated with simultaneous or sequential solution-based recovery of metals and other materials as described in more detail below.\|[0041] Further, excavation and formation of a permeability control impoundment can be accomplished simultaneously. For example, an excavator can be configured to remove hydrocarbonaceous material while side walls of an impoundment are formed. Material can be removed from just underneath edges of the side walls such that the walls can be guided downward to allow additional wall segments to be stacked above. This approach can allow for increased depths while avoiding or reducing dangers of cave-in prior to formation of supporting impoundment walls.\|[0042] The impoundment can be formed of any suitable material which provides isolation of material transfer across walls of the impoundment. In this manner, integrity of the walls is retained during operation of the control infrastructure sufficient to substantially prevent uncontrolled migration of fluids outside of the control infrastructure. Non-limiting examples of suitable material for use in forming the impoundment of the constructed permeability control infrastructure can include clay, bentonite clay (e.g. clay comprising at least a portion of bentonite), bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, or combinations thereof. Engineered cementitious composites (ECC) materials, fiber reinforced composites, and the like can be particularly strong and can be readily engineered to meet permeability and temperature tolerance requirements of a given installation. As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required. For example, materials having a melting point above the maximum operating temperature of the infrastructure can be useful to maintain containment during and after heating and recovery. However, lower temperature materials can also be used if a non-heated buffer zone is maintained between the walls and heated portions of the permeable body. Such buffer zones can range from 6 inches to 50 feet depending on the particular material used for the impoundment and the composition of the permeable body. In another aspect, walls of the impoundment can be acid, water, and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water. For impoundment walls formed along formations or other solid support, the impoundment walls can be formed of a sprayed grouting, sprayed liquid emulsions, or other sprayed material such as sprayable refractory grade grouting which forms a seal against the formation and creates the permeability control wall of the impoundments. Impoundment walls may be substantially continuous such that the impoundment defines the encapsulated volume sufficiently to prevent substantial movement of fluids into or out of the impoundment other than defined inlets and outlets, e.g. via conduits or the like as discussed herein. In this manner, the impoundments can readily meet government fluid migration regulations. Alternatively, or in combination with a manufactured barrier, portions of the impoundment walls can be undisturbed geological formation and/or compacted earth. In such cases, the constructed permeability control infrastructure is a combination of permeable and impermeable walls as described in more detail below.\|[0043] In one detailed aspect, a portion of hydro carbonaceous material, either pre- or post-processed, can be used as a cement fortification and/or cement base which are then poured in place to form portions or the entirety of walls of the control infrastructure. These materials can be formed in place or can be preformed and then assembled on site to form an integral impoundment structure. For example, the impoundment can be constructed by cast forming in place as a monolithic body, extrusion, stacking of preformed or precast pieces, concrete panels joined by a grout (cement, ECC, or other suitable material), inflated form, or the like. The forms can be built up against a formation or can be stand alone structures. Forms can be constructed of any suitable material such as, but not limited to, steel, wood, fiberglass, polymer, or the like. The forms can be assembled in place or may be oriented using a crane or other suitable mechanism. Alternatively, the constructed permeability control infrastructure can be formed of gabions and/or geosynthetic fabrics assembled in layers with compacted fill material. Optional binders can be added to enhance compaction of the permeability control walls. In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|[0044] Impoundment walls can optionally include non-permeable insulation and/or fines collection layers. These permeable layers can be oriented between the permeability control barrier and the permeable body. For example, a layer of hydrocarbonaceous comminuted material can be provided which allows fluids to enter, cool, and at least partially condense within the layer. Such permeable layer material can generally have a particle size smaller than the permeable body. Further, such hydrocarbonaceous material can remove fines from passing fluids via various attractive forces. In one embodiment, the construction of impoundment walls and floors can include multiple compacted layers of indigenous or manipulated low grade shale with any combination of sand, cement, fiber, plant fiber, nano carbons, crushed glass, reinforcement steel, engineered carbon reinforcement grid, calcium salts, and the like. In addition to such composite walls, designs which inhibit long term fluid and gas migration through additional impermeability engineering can be employed including, but not limited to, liners, geo-membranes, compacted soils, imported sand, gravel or rock and gravity drainage contours to move fluids and gases away from impervious layers to egress exits. Impoundment floor and wall construction, can, but need not comprise, a stepped up or stepped down slope or bench as the case of mining course may dictate following the optimal ore grade mining. In any such stepped up or down applications, floor leveling and containment wall construction can typically drain or slope to one side or to a specific central gathering area(s) for removal of fluids by gravity drainage assistance.\|[0045] Optionally, capsule wall and floor construction can include insulation which prevents heat transfer outside of the constructed infrastructure or outside of inner capsules or conduits within the primary constructed capsule containment. Insulation can comprise manufactured materials, cement or various materials other materials which are less thermally conductive than surrounding masses, i.e. permeable body, formation, adjacent infrastructures, etc. Thermally insulating barriers can also be formed within the permeable body, along impoundment walls, ceilings, and/or floors. One detailed aspect includes the use of biodegradable insulating materials, e.g. soy insulation and the like. This is consistent with embodiments wherein the impoundment is a single use system such that insulations, pipes, and/or other components can have a relatively low useful life, e.g. less than 1-2 years. This can reduce equipment costs as well as reduce long-term environmental impact.\|[0046] These structures and methods can be applied at almost any scale. Larger encapsulated volumes and increased numbers of impoundments can readily produce hydrocarbon products and performance comparable to or exceeding smaller constructed infrastructures. As an illustration, single impoundments can range in size from tens of meters across to tens of acres. Optimal impoundment sizes may vary depending on the hydrocarbonaceous material and operating parameters, however it is expected that suitable areas can range from about one-half to five acres in top plan surface area.\|[0047] The methods and infrastructures can be used for recovery of hydrocarbons from a variety of hydrocarbonaceous materials. One particular advantage is a wide degree of latitude in controlling particle size, conditions, and composition of the permeable body introduced into the encapsulated volume. Non-limiting examples of mined hydrocarbonaceous material which can be treated comprise oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof. In some cases it can be desirable to provide a single type of hydro carbonaceous material so that the permeable body consists essentially of one of the above materials. However, the permeable body can include mixtures of these materials such that grade, oil content, hydrogen content, permeability and the like can be adjusted to achieve a desired result. Further, different hydrocarbon materials can be placed in multiple layers or in a mixed fashion such as combining coal, oil shale, tar sands, biomass, and/or peat.\|[0048] In one embodiment, hydrocarbon containing material can be classified into various inner capsules within a primary constructed infrastructure for optimization reasons. For instance, layers and depths of mined oil shale formations may be richer in certain depth pay zones as they are mined. Once blasted, mined, shoveled, and hauled inside of capsule for placement, richer oil bearing ores can be classified or mixed by richness for optimal yields, faster recovery, or for optimal averaging within each impoundment. Further, providing layers of differing composition can have added benefits. For example, a lower layer of tar sands can be oriented below an upper layer of oil shale. Generally, the upper and lower layers can be in direct contact with one another although this is not required. The upper layer can include heating pipes embedded therein as described in more detail below. The heating pipes can heat the oil shale sufficient to liberate kerogen oil, including short-chain liquid hydrocarbons, which can act as a solvent for bitumen removal from the tar sands. In this manner, the upper layer acts as an in situ solvent source for enhancing bitumen removal from the lower layer. Heating pipes within the lower layer are optional such that the lower layer can be free of heating pipes or may include heating pipes, depending on the amount of heat transferred via downward passing liquids from the upper layer and any other heat sources. The ability to selectively control the characteristics and composition of the permeable body adds a significant amount of freedom in optimizing oil yields and quality.\|[0049] Furthermore, in many embodiments, the liberated gaseous and liquid products act as an in situ produced solvent which supplements kerogen removal and/or additional hydrocarbon removal from the hydrocarbonaceous material.\|[0050] In yet another detailed aspect, the permeable body can further comprise an additive or biomass. Additives can include any composition which acts to increase the quality of removed hydrocarbons, e.g. increased API, decreased viscosity, improved flow properties, reduced wetting of residual shale, reduction of sulfur, hydrogenation agents, etc. Non-limiting examples of suitable additives can include bitumen, kerogen, propane, natural gas, natural gas condensate, crude oil, refining bottoms, asphaltenes, common solvents, other diluents, and combinations of these materials. In one specific embodiment, the additive can include a flow improvement agent and/or a hydrogen donor agent. Some materials can act as both or either agents to improve flow or as a hydrogen donor. Non-limiting examples of such additives can include methane, natural gas condensates, common solvent such as acetone, toluene, benzene, etc., and other additives listed above. Additives can act to increase the hydrogen to carbon ratio in any hydrocarbon products, as well as act as a flow enhancement agent. For example, various solvents and other additives can create a physical mixture which has a reduced viscosity and/or reduced affinity for particulate solids, rock, and the like. Further, some additives can chemically react with hydrocarbons and/or allow liquid flow of the hydrocarbon products. Any additives used can become part of a final recovered product or can be removed and reused or otherwise disposed of.\|[0051] Similarly, biological hydroxylation of hydrocarbonaceous materials to form synthetic gas or other lighter weight products can be accomplished using known additives and approaches. Enzymes or biocatalysts can also be used in a similar manner. Further, manmade materials can also be used as additives such as, but not limited to, tires, polymeric refuse, or other hydrocarbon-containing materials.\|[0052] Although these methods are broadly applicable, as a general guideline, the permeable body can include particles from about ⅛ inch to about 6 feet in largest dimension, and in some cases less than 1 foot and in other cases less than about 6 inches. However, as a practical matter, sizes from about 2 inches to about 2 feet can provide good results with about 1 foot diameter being useful for oil shale especially. Void space can be an important factor in determining optimal particle diameters. As a general matter, any functional void space can be used; however, about 10% to about 50% and in some cases about 30% to about 45% usually provides a good balance of permeability and effective use of available volumes. Void volumes can be varied somewhat by varying other parameters such as heating conduit placement, additives, and the like. Mechanical separation of mined hydrocarbonaceous materials allows creation of fine mesh, high permeability particles which enhance thermal dispersion rates once placed in capsule within the impoundment. The added permeability allows for more reasonable, low temperatures which also help to avoid higher temperatures which result in greater CO2 production from carbonate decomposition and associated release of trace heavy metals, volatile organics, and other compounds which can create toxic effluent and/or undesirable materials which are monitored and controlled.\|[0053] Carbon dioxide that is produced during the recovery process can be sequestered using one or more approaches. In particular, carbon dioxide can be converted to a solid or liquid form such that the associated carbon is precipitated or otherwise converted to a useful product. Such sequestering can be optionally accomplished by reacting carbon dioxide with an aqueous solution to form a precipitation of carbon dioxide with a metal. When referring to carbon dioxide precipitates or precipitating carbon dioxide, it is understood that precipitation consumes the carbon dioxide such that the carbon dioxide no longer exists as a CO2 structure. As such, the process is generally irreversible and differs from general adsorption techniques, which can also be used for sequestering carbon dioxide as further described herein. In one embodiment, the aqueous solution can be an ionic solution. In another embodiment, the aqueous solution can be salt water. The metal can be any metal that is capable of forming a solid with carbon dioxide including oxides thereof. In one embodiment, the metal can be calcium, magnesium, including oxides thereof, silicates thereof, and mixtures thereof. In one embodiment, the metal can be in the form of forsterite, serpentine and/or peridotite. In one embodiment, the exhausted hydrocarbonaceous materials can be injected or admixed with the carbon dioxide and salt water to form carbon dioxide precipitates. Such a process can take advantage of metals found in the exhausted hydrocarbonaceous materials.\|[0054] Additionally, other materials can be added to increase the reaction kinetics to form the carbon dioxide precipitate. For example, the addition of acids, catalysts, or other organic compounds may increase the reaction kinetics. Such sequestering can also produce heat during the sequestering process. In one embodiment, the heat can be redirected and applied to the heating step as discussed herein. Such recycling of heat can further provide a more efficient recovery system.\|[0055] Additionally, or alternatively, sequestering of carbon dioxide can be achieved by cryogenic precipitation forming liquid carbon dioxide. The collected carbon dioxide can be liquefied by lowering the temperature. Such liquid carbon dioxide can then be transferred to a container for disposal or for reuse. In one embodiment, the liquid carbon dioxide can be reacted to form polycarbonates, which can provide a stable form for disposal or potential use in other industries. In another embodiment, the liquid carbon dioxide can be used to further process the exhausted hydrocarbonaceous materials, as further discussed herein, including rinsing the hydrocarbonaceous materials during the recovery process. Such treatment can provide additional recovery of hydrocarbons that have not been removed during the initial recovery process as described herein.\|[0056] The sequestered carbon dioxide can be used in other commercial processes. In one embodiment, carbon dioxide can be used to isolate polymers from fluids. For example, carbon dioxide can be used to isolate polycarbonates from a solvent, e.g. methylene chloride. In another embodiment, carbon dioxide can be pumped into depleted permeable bodies. In the case of permeable bodies having a high coal content, once the initial stores of methane or other products are recovered, CO2 can be pumped into the impoundment, where it is stored in the coal, which can then provide the benefit of releasing additional methane. Between three and thirteen molecules of CO2 can be absorbed for each molecule of methane, making coal an excellent storage location for CO2.\|[0057] In one embodiment, storage of carbon dioxide can be performed in deep saline aquifers or brine-saturated rock formations that occur deep underground or under the ocean. Specifically, wells deep underground consisting of porous rock, such as limestone or sandstone, saturated with saltwater can form an effective trap for injected CO2. Geologically, over time, some CO2 can react with rock minerals to form solid carbonates, further immobilizing the same.\|[0058] Additionally, a liquid carbon dioxide can be optionally mixed and/or adsorbed by the exhausted hydrocarbonaceous materials. Such materials can then be disposed in an appropriate manner. When referring to liquid carbon dioxide, the embodiments herein can also be used with supercritical carbon dioxide. As such, the discussion and embodiments presented herein referring to liquid carbon dioxide also can be applied with respect to supercritical carbon dioxide.\|[0059] In another embodiment, sequestering carbon dioxide can be achieved by injecting exhausted hydrocarbonaceous materials with the carbon dioxide. Such injection can provide adsorption of carbon dioxide. Additionally, such process can be performed with a catalyst or without a catalyst. Other metal and organic additives can be included as discussed herein. In one embodiment, such sequestering can include a metal selected from the group consisting of calcium, magnesium, including oxides thereof, silicates thereof, and mixtures thereof.\|[0060] With respect to carbon dioxide sequestering, a constructed permeability control infrastructure can comprise a permeability control impoundment defining a substantially encapsulated volume wherein the permeability control impoundment is substantially free of undisturbed geological formations, a comminuted hydrocarbonaceous material within the encapsulated volume forming a permeable body of hydrocarbonaceous material, and a carbon dioxide collection unit operatively connected to collect carbon dioxide from the control infrastructure. It is understood that the infrastructure can include any of the elements described herein including those elements that have been referred to in the context of a process. Additionally, the methods and processes described herein can include any elements described herein including those elements that have been referred to in the context of a composition or system.\|[0061] The carbon dioxide can be collected consistent with one or more of the above approaches using a corresponding carbon dioxide control unit. In one optional aspect, the carbon dioxide control unit can include a vessel for treatment and/or storage of the carbon dioxide. Additional storage tanks, pumps and/or vessels can also be used for transporting or storage of treatment chemicals and by-products. As described herein, the vessel can contain an aqueous solution, a metal, and carbon dioxide where the vessel is configured to react the carbon dioxide with the aqueous solution to form a precipitation of carbon dioxide with the metal. In another embodiment, the vessel can contain carbon dioxide where the vessel is configured to form liquid carbon dioxide from the carbon dioxide by cryogenic precipitation. Additionally, the vessel can contain exhausted hydrocarbonaceous materials that adsorb the liquid carbon dioxide. In one embodiment, the vessel can contain carbon dioxide where the vessel is configured to mix exhausted hydrocarbonaceous materials with the carbon dioxide such that the exhausted hydrocarbonaceous materials adsorb the carbon dioxide.\|[0062] In one embodiment, computer assisted mining, mine planning, hauling, blasting, assay, loading, transport, placement, and dust control measures can be utilized to fill and optimize the speed of mined material movement into the constructed capsule containment structure. In one alternative aspect, the impoundments can be formed in excavated volumes of a hydrocarbonaceous formation, although other locations remote from the control infrastructure can also be useful. For example, some hydrocarbonaceous formations have relatively thin hydrocarbon-rich layers, e.g. less than about 300 feet thick. Therefore, vertical mining and drilling tend to not be cost effective. In such cases, horizontal mining can be useful to recover the hydrocarbonaceous materials for formation of the permeable body. Although horizontal mining continues to be a challenging endeavor, a number of technologies have been developed and continue to be developed which can be useful in connection with the impoundments. In such cases, at least a portion of the impoundment can be formed across a horizontal layer, while other portions of the impoundment can be formed along and/or adjacent non-hydrocarbon bearing formation layers. Other mining approaches such as, but not limited to, room and pillar mining can provide an effective source of hydrocarbonaceous material with minimal waste and/or reclamation which can be transported to an impoundment and treated in accordance with the these principles.\|[0063] As mentioned herein, these systems and processes allow for a large degree of control regarding properties and characteristics of the permeable body which can be designed and optimized for a given installation. Impoundments, individually and across a plurality of impoundments can be readily tailored and classified based on varying composition of materials, intended products and the like. For example, several impoundments can be dedicated to production of heavy crude oil, while others can be configured for production of lighter products and/or syn gas. Non-limiting example of potential classifications and factors can include catalyst activity, enzymatic reaction for specific products, aromatic compounds, hydrogen content, microorganism strain or purpose, upgrading process, target final product, pressure (effects product quality and type), temperature, swelling behavior, aquathermal reactions, hydrogen donor agents, heat superdisposition, garbage impoundment, sewage impoundment, reusable pipes, and others. Typically, a plurality of these factors can be used to configure impoundments in a given project area for distinct products and purposes.\|[0064] The comminuted hydrocarbonaceous material can be filled into the control infrastructure to form the permeable body in any suitable manner. Typically the comminuted hydrocarbonaceous material can be conveyed into the control infrastructure by dumping, conveyors or other suitable approaches. As mentioned previously, the permeable body can have a suitably high void volume. Indiscriminate dumping can result in excessive compaction and reduction of void volumes. Thus, the permeable body can be formed by low compaction conveying of the hydrocarbonaceous material into the infrastructure. For example, retracting conveyors can be used to deliver the material near a top surface of the permeable body as it is formed. In this way, the hydrocarbonaceous material can retain a significant void volume between particles without substantial further crushing or compaction despite some small degree of compaction which often results from lithostatic pressure as the permeable body is formed.\|[0065] Once a desired permeable body has been formed within the control infrastructure, heat can be introduced sufficient to begin removal of hydrocarbons, e.g. via pyrolysis. A suitable heat source can be thermally associated with the permeable body. Optimal operating temperatures within the permeable body can vary depending on the composition and desired products. However, as a general guideline, operating temperatures can range from about 200° F. to about 750° F. Temperature variations throughout the encapsulated volume can vary and may reach as high as 900° F. or more in some areas. In one embodiment, the operating temperature can be a relatively lower temperature to facilitate production of liquid product such as from about 200° F. to about 650° F. This heating step can be a roasting operation which results in beneficiation of the crushed ore of the permeable body. Further, one embodiment comprises controlling the temperature, pressure and other variables sufficient to produce predominantly, and in some cases substantially only, liquid product. Generally, products can include both liquid and gaseous products, while liquid products can require fewer processing steps such as scrubbers etc. The relatively high permeability of the permeable body allows for production of liquid hydrocarbon products and minimization of gaseous products, depending to some extent on the particular starting materials and operating conditions. In one embodiment, the recovery of hydrocarbon products can occur substantially in the absence of cracking within the permeable body.\|[0066] In one aspect, heat can be transferred to the permeable body via convection. Heated gases can be injected into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body. Heated gases can be produced by combustion of natural gas, hydrocarbon product, or any other suitable source. Non-limiting examples of suitable heat transfer fluids can include hot air, hot exhaust gases, steam, hydrocarbon vapors and/or hot liquids. The heated gases can be imported from external sources or recovered from the process.\|[0067] Alternatively, or in combination with convective heating, a highly configurable approach can include embedding a plurality of conduits within the permeable body. The conduits can be configured for use as heating pipes, cooling pipes, heat transfer pipes, drainage pipes, or gas pipes. Further, the conduits can be dedicated to a single function or may serve multiple functions during operation of the infrastructure, i.e. heat transfer and drainage. The conduits can be formed of any suitable material, depending on the intended function. Non-limiting examples of suitable materials can include clay pipes, refractory cement pipes, refractory ECC pipes, poured in place pipes, metal pipes such as cast iron, stainless steel etc., polymer such as PVC, and the like. In one specific embodiment, all or at least a portion of the embedded conduits can comprise a degradable material. For example, non-galvanized 6″ cast iron pipes can be effectively used for single use embodiments and perform well over the useful life of the impoundment, typically less than about 2 years. Further, different portions of the plurality of conduits can be formed of different materials. Poured in place pipes can be especially useful for very large encapsulation volumes where pipe diameters exceed several feet. Such pipes can be formed using flexible wraps which retain a viscous fluid in an annular shape. For example, PVC pipes can be used as a portion of a form along with flexible wraps, where concrete or other viscous fluid is pumped into an annular space between the PVC and flexible wrap. Depending on the intended function, perforations or other apertures can be made in the conduits to allow fluids to flow between the conduits and the permeable body. Typical operating temperatures exceed the melting point of conventional polymer and resin pipes. In some embodiments, the conduits can be placed and oriented such that the conduits intentionally melt or otherwise degrade during operation of the infrastructure.\|[0068] The plurality of conduits can be readily oriented in any configuration, whether substantially horizontal, vertical, slanted, branched, or the like. At least a portion of the conduits can be oriented along predetermined pathways prior to embedding the conduits within the permeable body. The predetermined pathways can be designed to improve heat transfer, gas-liquid-solid contacting, maximize fluid delivery or removal from specific regions within the encapsulated volume, or the like. Further, at least a portion the conduits can be dedicated to heating of the permeable body. These heating conduits can be selectively perforated to allow heated gases or other fluids to convectively heat and mix throughout the permeable body. The perforations can be located and sized to optimize even and/or controlled heating throughout the permeable body. Alternatively, the heating conduits can form a closed loop such that heating gases or fluids are segregated from the permeable body. Thus, a “closed loop” does not necessarily require recirculation, rather isolation of heating fluid from the permeable body. In this manner, heating can be accomplished primarily or substantially only through thermal conduction across the conduit walls from the heating fluids into the permeable body. Heating in a closed loop allows for prevention of mass transfer between the heating fluid and permeable body and can reduce formation and/or extraction of gaseous hydrocarbon products.\|[0069] During the heating or roasting of the permeable body, localized areas of heat which exceed parent rock decomposition temperatures, often above about 900° F., can reduce yields and form carbon dioxide and undesirable contaminating compounds which can lead to leachates containing heavy metals, soluble organics and the like. The heating conduits can allow for substantial elimination of such localized hot spots while maintaining a vast majority of the permeable body within a desired temperature range. The degree of uniformity in temperature can be a balance of cost (e.g. for additional heating conduits) versus yields. However, at least about 85% of the permeable body can readily be maintained within about 5-10% of a target temperature range with substantially no hot spots, i.e. exceeding the decomposition temperature of the hydrocarbonaceous materials such as about 800° F. and in many cases about 900° F. Thus, operated as described herein, the systems can allow for recovery of hydrocarbons while eliminating or substantially avoiding production of undesirable leachates. Although products can vary considerably depending on the starting materials, high quality liquid and gaseous products are possible. In accordance with one embodiment, a crushed oil shale material can produce a liquid product having an API from about 30 to about 45, with about 33 to about 38 being currently typical, directly from the oil shale without additional treatment. Interestingly, practice of these processes has led to an understanding that pressure appears to be a much less influential factor on the quality of recovered hydrocarbons than temperature and heating times. Although heating times can vary considerably, depending on void space, permeable body composition, quality, etc., as a general guideline times can range from a few days (i.e. 3-4 days) up to about one year. In one specific example, heating times can range from about 2 weeks to about 4 months. Under-heating oil shale at short residence times, i.e. minutes to several hours, can lead to formation of leachable and/or somewhat volatile hydrocarbons. Accordingly, these systems and methods allow for extended residence times at moderate temperatures such that organics present in oil shale can be volatilized and/or carbonized, leaving insubstantial leachable organics. In addition, the underlying shale is not generally decomposed or altered which reduces soluble salt formation.\|[0070] Further, conduits can be oriented among a plurality of impoundments and/or control infrastructures to transfer fluids and/or heat between the structures. The conduits can be welded to one another using conventional welding or the like. Further, the conduits can include junctions which allow for rotation and or small amounts of movement during expansion and subsidence of material in the permeable body. Additionally, the conduits can include a support system which acts to support the assembly of conduits prior to and during filling of the encapsulated volume, as well as during operation. For example, during heating flows of fluids, heating and the like can cause expansion (fracturing or popcorn effect) or subsidence sufficient to create potentially damaging stress and strain on the conduits and associated junctions. A truss support system or other similar anchoring members can be useful in reducing damage to the conduits. The anchoring members can include cement blocks, 1-beams, rebar, columns, etc. which can be associated with walls of the impoundment, including side walls, floors and ceilings.\|[0071] Alternatively, the conduits can be completely constructed and assembled prior to introduction of any mined materials into the encapsulated volume. Care and planning can be considered in designing the predetermined pathways of the conduits and method of filling the volume in order to prevent damage to the conduits during the filling process as the conduits are buried. Thus, as a general rule, the conduits are oriented ab initio, or prior to embedding in the permeable body such that they are non-drilled. As a result, construction of the conduits and placement thereof can be performed without extensive core drilling and/or complicated machinery associated with well-bore or horizontal drilling. Rather, horizontal or any other orientation of conduit can be readily achieved by assembling the desired predetermined pathways prior to, or contemporaneous with, filling the infrastructure with the mined hydrocarbonaceous material. The non-drilled, hand/crane-placed conduits oriented in various geometric patterns can be laid with valve controlled connecting points which yield precise and closely monitored heating within the capsule impoundment. The ability to place and layer conduits including connecting, bypass and flow valves, and direct injection and exit points, allow for precision temperature and heating rates, precision pressure and pressurization rates, and precision fluid and gas ingress, egress and composition admixtures. For example, when a bacteria, enzyme, or other biological material is used, optimal temperatures can be readily maintained throughout the permeable body to increase performance, reaction, and reliability of such biomaterials.\|[0072] The conduits will generally pass through walls of the constructed infrastructure at various points. Due to temperature differences and tolerances, it can be beneficial to include an insulating material at the interface between the wall and the conduits. The dimensions of this interface can be minimized while also allowing space for thermal expansion differences during startup, steady-state operation, fluctuating operating conditions, and shutdown of the infrastructure. The interface can also involve insulating materials and sealant devices which prevent uncontrolled egress of hydrocarbons or other materials from the control infrastructure. Non-limiting examples of suitable materials can include high temperature gaskets, metal alloys, ceramics, clay or mineral liners, composites or other materials which having melting points above typical operating temperatures and act as a continuation of the permeability control provided by walls of the control infrastructure.\|[0073] Further, walls of the constructed infrastructure can be configured to minimize heat loss. In one aspect, the walls can be constructed having a substantially uniform thickness which is optimized to provide sufficient mechanical strength while also minimizing the volume of wall material through which the conduits pass. Specifically, excessively thick walls can reduce the amount of heat which is transferred into the permeable body by absorbing the same through conduction. Conversely, the walls can also act as a thermal barrier to somewhat insulate the permeable body and retain heat therein during operation.\|[0074] In one embodiment, fluid and gas compounds within the permeable body can be altered for desired extractive products using, as an example, induced pressure through gases or piled lithostatic pressure from piled rubble. Thus, some degree of upgrading and/or modification can be accomplished simultaneous with the recovery process. Further, certain hydro carbonaceous materials can require treatment using specific diluents or other materials. For example, treatment of tar sands can be readily accomplished by steam injection or solvent injection to facilitate separation of bitumen from sand particles according to well known mechanisms.\|[0075] With the above description in mind, FIG. 1 depicts a side view of one embodiment showing an engineered capsule containment and extraction impoundment 100 where existing grade 108 is used primarily as support for the impermeable floor layer 112. Exterior capsule impoundment side walls 102 provide containment and can, but need not be, subdivided by interior walls 104. Subdividing can create separate containment capsules 122 within a greater capsule containment of the impoundment 100 which can be any geometry, size or subdivision. Further subdivisions can be horizontally or vertically stacked. By creating separate containment capsules 122 or chambers, classification of lower grade materials, varied gases, varied liquids, varied process stages, varied enzymes or microbiology types, or other desired and staged processes can be readily accommodated. Sectioned capsules constructed as silos within larger constructed capsules can also be designed to provide staged and sequenced processing, temperatures, gas and fluid compositions and thermal transfers. Such sectioned capsules can provide additional environmental monitoring and can be built of lined and engineered tailings berms similar to the primary exterior walls. In one embodiment, sections within the impoundment 100 can be used to place materials in isolation, in the absence of external heat, or with the intent of limited or controlled combustion or solvent application. Lower content hydrocarbon bearing material can be useful as a combustion material or as fill or a berm wall building material. Material which does not meet a various cut-off grade thresholds can also be sequestered without alteration in an impoundment dedicated for such purpose. In such embodiments, such areas may be completely isolated or bypassed by heat, solvents, gases, liquids, or the like. Optional monitoring devices and/or equipment can be permanently or temporarily installed within the impoundment or outside perimeters of the impoundments in order to verify containment of the sequestered material.\|[0076] Walls 102 and 104 as well as cap 116 and impermeable layer 112 can be engineered and reinforced by gabions 146 and or geogrid 148 layered in fill compaction. Alternatively, these walls 102, 104, 116 and 112 which comprise the permeability control impoundment and collectively define the encapsulated volume can be formed of any other suitable material as previously described. In this embodiment, the impoundment 100 includes side walls 102 and 104 which are self-supporting. In one embodiment, tailings berms, walls, and floors can be compacted and engineered for structure as well as permeability. The use of compacted geogrids and other deadman structures for support of berms and embankments can be included prior to or incorporated with permeability control layers which may include sand, clay, bentonite clay, gravel, cement, grout, reinforced cement, refractory cements, insulations, geo-membranes, drainpipes, temperature resistant insulations of penetrating heated pipes, etc.\|[0077] In one alternative embodiment, the permeability control impoundment can include side walls which are compacted earth and/or undisturbed geological formations while the cap and floors are impermeable. Specifically, in such embodiments an impermeable cap can be used to prevent uncontrolled escape of volatiles and gases from the impoundment such that appropriate gas collection outlets can be used. Similarly, an impermeable floor can be used to contain and direct collected liquids to a suitable outlet such the drain system 133 to remove liquid products from lower regions of the impoundment. Although impermeable side walls can be desirable in some embodiments, such are not always required. In some cases, side walls can be exposed undisturbed earth or compacted fill or earth, or other permeable material. Having permeable side walls may allow some small egress of gases and/or liquids from the impoundment.\|[0078] Although not shown, above, below, around and adjacent to constructed capsule containment vessels environmental hydrology measures can be engineered to redirect surface water away from the capsule walls, floors, caps, etc. during operation. Further, gravity assisted drainage pipes and mechanisms can be utilized to aggregate and channel fluids, liquids or solvents within the encapsulated volume to central gathering, pumping, condensing, heating, staging and discharge pipes, silos, tanks, and/or wells as needed. In a similar manner, steam and/or water which is intentionally introduce, e.g. for tar sands bitumen treatment, can be recycled.\|[0079] Once wall structures 102 and 104 have been constructed above a constructed and impermeable floor layer 112 which commences from ground surface 106, the mined rubble 120 (which may be crushed or classified according to size or hydrocarbon richness), can be placed in layers upon (or next to) placed tubular heating pipes 118, fluid drainage pipes 124, and, or gas gathering or injection pipes 126. These pipes can be oriented and designed in any optimal flow pattern, angle, length, size, volume, intersection, grid, wall sizing, alloy construction, perforation design, injection rate, and extraction rate. In some cases, pipes such as those used for heat transfer can be connected to, recycled through or derive heat from heat source 134. Alternatively, or in combination with, recovered gases can be condensed by a condenser 140. Heat recovered by the condenser can be optionally used to supplement heating of the permeable body or for other process needs.\|[0080] Heat source 134 can derive, amplify, gather, create, combine, separate, transmit or include heat derived from any suitable heat source including, but not limited to, fuel cells (e.g. solid oxide fuel cells, molten carbonate fuel cells and the like), solar sources, wind sources, hydrocarbon liquid or gas combustion heaters, geothermal heat sources, nuclear power plant, coal fired power plant, radio frequency generated heat, wave energy, flameless combustors, natural distributed combustors, or any combination thereof. In some cases, electrical resistive heaters or other heaters can be used, although fuel cells and combustion-based heaters are particularly effective. In some locations, geothermal water can be circulated to the surface in adequate amounts to heat the permeable body and directed into the infrastructure.\|[0081] In another embodiment, electrically conductive material can be distributed throughout the permeable body and an electric current can be passed through the conductive material sufficient to generate heat. The electrically conductive material can include, but is not limited to, metal pieces or beads, conductive cement, metal coated particles, metal-ceramic composites, conductive semi-metal carbides, calcined petroleum coke, laid wire, combinations of these materials, and the like. The electrically conductive material can be premixed having various mesh sizes or the materials can be introduced into the permeable body subsequent to formation of the permeable body.\|[0082] Liquids or gases can transfer heat from heat source 134, or in another embodiment, in the cases of hydrocarbon liquid or gas combustion, radio frequency generators (microwaves), or fuel cells all can, but need not, actually generate heat inside of capsule impoundment area 114 or 122. In one embodiment, heating of the permeable body can be accomplished by convective heating from hydrocarbon combustion. Of particular interest is hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen. Stoichiometric conditions can allow for significantly increased heat gas temperatures. Stoichiometric combustion can employ but does not generally require a pure oxygen source which can be provided by known technologies including, but not limited to, oxygen concentrators, membranes, electrolysis, and the like. In some embodiments oxygen can be provided from air with stoichiometric amounts of oxygen and hydrogen. Combustion off gas can be directed to an ultra-high temperature heat exchanger, e.g. a ceramic or other suitable material having an operating temperature above about 2500° F. Air obtained from ambient or recycled from other processes can be heated via the ultra high temperature heat exchanger and then sent to the impoundment for heating of the permeable body. The combustion off gases can then be sequestered without the need for further separation, i.e. because the off gas is predominantly carbon dioxide and water.\|[0083] In order to minimize heat losses, distances can be minimized between the combustion chamber, heat exchanger, and impoundments. Therefore, in one specific detailed embodiment portable combustors can be attached to individual heating conduits or smaller sections of conduits. Portable combustors or burners can individually provide from about 100,000 Btu to about 1,000,000 Btu with about 600,000 Btu per pipe generally being sufficient.\|[0084] Alternatively, in-capsule combustion can be initiated inside of isolated capsules within a primary constructed capsule containment structure. This process partially combusts hydrocarbonaceous material to provide heat and intrinsic pyrolysis. Unwanted air emissions 144 can be captured and sequestered in a formation 108 once derived from capsule containment 114, 122 or from heat source 134 and delivered by a drilled well bore 142. Heat source 134 can also create electricity and transmit, transform or power via electrical transmission lines 150. The liquids or gases extracted from capsule impoundment treatment area 114 or 122 can be stored in a nearby holding tank 136 or within a capsule containment 114 or 122. For example, the impermeable floor layer 112 can include a sloped area 110 which directs liquids towards drain system 133 where liquids are directed to the holding tank.\|[0085] As rubble material 120 is placed with piping 118, 124, 126, and 128, various measurement devices or sensors 130 are envisioned to monitor temperature, pressure, fluids, gases, compositions, heating rates, density, and all other process attributes during the extractive process within, around, or underneath the engineered capsule containment impoundment 100. Such monitoring devices and sensors 130 can be distributed anywhere within, around, part of, connected to, or on top of placed piping 118, 124, 126, and 128 or, on top of, covered by, or buried within rubble material 120 or impermeable barrier zone 112.\|[0086] As placed rubble material 120 fills the capsule treatment area 114 or 122, 120 becomes the ceiling support for engineered impermeable cap barrier zone 138, and wall barrier construction 170, which may include any combination of impermeability and engineered fluid and gas barrier or constructed capsule construction comprising those which may make up 112 including, but not limited to clay 162, compacted fill or import material 164, cement or refractory cement containing material 166, geo synthetic membrane, liner or insulation 168. Above 138, fill material which can be oriented as ceiling cap 116 is placed to create lithostatic pressure upon the capsule treatment areas 114 or 122. Covering the permeable body with compacted fill sufficient to create an increased lithostatic pressure within the permeable body can be useful in further increasing hydrocarbon product quality. A compacted fill ceiling can substantially cover the permeable body, while the permeable body in return can substantially support the compacted fill ceiling. The compacted fill ceiling can further be sufficiently impermeable to removed hydrocarbon or an additional layer of permeability control material can be added in a similar manner as side and/or floor walls. Additional pressure can be introduced into extraction capsule treatment area 114 or 122 by increasing any gas or fluid once extracted, treated or recycled, as the case may be, via any of piping 118, 124, 126, or 128. All relative measurements, optimization rates, injection rates, extraction rates, temperatures, heating rates, flow rates, pressure rates, capacity indicators, chemical compositions, or other data relative to the process of heating, extraction, stabilization, sequestration, impoundment, upgrading, refining or structure analysis within the capsule impoundment 100 are envisioned through connection to a computing device 132 which operates computer software for the management, calculation and optimization of the entire process. Further, core drilling, geological reserve analysis and assay modeling of a formation prior to blasting, mining and hauling (or at any time before, after or during such tasks) can serve as data input feeds into computer controlled mechanisms that operate software to identify optimal placements, dimensions, volumes and designs calibrated and cross referenced to desired production rate, pressure, temperature, heat input rates, gas weight percentages, gas injection compositions, heat capacity, permeability, porosity, chemical and mineral composition, compaction, density. Such analysis and determinations may include other factors like weather data factors such as temperature and air moisture content impacting the overall performance of the constructed infrastructure. Other data such as ore moisture content, hydrocarbon richness, weight, mesh size, and mineral and geological composition can be utilized as inputs including time value of money data sets yielding project cash flows, debt service, and internal rates of return.\|[0087] FIG. 2A shows a collection of impoundments including an uncovered or uncapped capsule impoundment 100, containing sectioned capsule impoundments 122 inside of a mining quarry 200 with various elevations of bench mining. FIG. 2B illustrates a single impoundment 122 without associated conduits and other aspects merely for clarity. This impoundment can be similar to that illustrated in FIG. 1 or any other configuration. In some embodiments, it is envisioned that mining rubble can be transferred down chutes 230 or via conveyors 232 to the quarry capsule impoundments 100 and 122 without any need of mining haul trucks.\|[0088] FIG. 3 shows the engineered permeability barriers 112 below capsule impoundment 100 resting on existing grade 106 of formation 108 with cap covering material or fill 302 on the sides and top of capsule impoundment 100 to ultimately (following the process) cover and reclaim a new earth surface 300. Indigenous plants which may have been temporarily moved from the area may be replanted such as trees 306. The constructed infrastructures can generally be single use structures which can be readily and securely shut down with minimal additional remediation. This can dramatically reduce costs associated with moving large volumes of spent materials. However, in some circumstances the constructed infrastructures can be excavated and reused. Some equipment such as radio frequency (RF) mechanisms, tubulars, devices, and emitters may be recovered from within the constructed impoundment upon completion of hydrocarbon recovery.\|[0089] FIG. 4 shows computer means 130 controlling various property inputs and outputs of conduits 118, 126, or 128 connected to heat source 134 during the process among the subdivided impoundments 122 within a collective impoundment 100 to control heating of the permeable body. Similarly, liquid and vapor collected from the impoundments can be monitored and collected in tank 136 and condenser 140, respectively. Condensed liquids from the condenser can be collected in tank 141, while non-condensable vapor collected at unit 143. As described previously, the liquid and vapor products can be combined or more often left as separate products depending on condensability, target product, and the like. A portion of the vapor product can be optionally condensed and combined with the liquid products in tank 136. However, much of the vapor product will be C4 and lighter gases which can be burned, sold, or used within the process. For example, hydrogen gas may be recovered using conventional gas separation and used to hydrotreat the liquid products according to conventional upgrading methods, e.g. catalytic, etc. or the non-condensable gaseous product can be burned to produce heat for use in heating the permeable body, heating an adjacent or nearby impoundment, heating service or personnel areas, or satisfying other process heat requirements. The constructed infrastructure can include thermocouples, pressure meters, flow meters, fluid dispersion sensors, richness sensors and any other conventional process control devices distributed throughout the constructed infrastructure. These devices can be each operatively associated with a computer such that heating rates, product flow rates, and pressures can be monitored or altered during heating of the permeable body. Optionally, in-place agitation can be performed using, for example, ultrasonic generators which are associated with the permeable body. Such agitation can facilitate separation and pyrolysis of hydrocarbons from the underlying solid materials with which they are associated. Further, sufficient agitation can reduce clogging and agglomeration throughout the permeable body and the conduits.\|[0090] FIG. 5 shows how any of the conduits can be used to transfer heat in any form of gas, liquid or heat via transfer means 510 from any sectioned capsule impoundment to another. Then, cooled fluid can be conveyed via heat transfer means 512 to the heat originating capsule 500, or heat originating source 134 to pick up more heat from capsule 500 to be again recirculated to a destination capsule 522. Thus, various conduits can be used to transfer heat from one impoundment to another in order to recycle heat and manage energy usage to minimize energy losses.\|[0091] In yet another aspect, a hydrogen donor agent can be introduced into the permeable body during the step of heating. The hydrogen donor agent can be any composition which is capable of hydrogenation of the hydrocarbons and can optionally be a reducing agent. Non-limiting examples of suitable hydrogen donor agents can include synthesis gas, propane, methane, hydrogen, natural gas, natural gas condensate, industrial solvents such as acetones, toluenes, benzenes, xylenes, cumenes, cyclopentanes, cyclohexanes, lower alkenes (C4-C10), terpenes, substituted compounds of these solvents, etc., and the like. Further, the recovered hydrocarbons can be subjected to hydrotreating either within the permeable body or subsequent to collection. Advantageously, hydrogen recovered from the gas products can be reintroduced into the liquid product for upgrading. Regardless, hydrotreating or hydrodesulfurization can be very useful in reducing nitrogen and sulfur content in final hydrocarbon products. Optionally, catalysts can be introduced to facilitate such reactions. In addition, introduction of light hydrocarbons into the permeable body can result in reforming reactions which reduce the molecular weight, while increasing the hydrogen to carbon ratio. This is particularly advantageous due at least in part to high permeability of the permeable body, e.g. often around 30%-40% void volume although void volume can generally vary from about 10% to about 50% void volume. Light hydrocarbons which can be injected can be any which provide reforming to recovered hydrocarbons. Non-limiting examples of suitable light hydrocarbons include natural gas, natural gas condensates, industrial solvents, hydrogen donor agents, and other hydrocarbons having ten or fewer carbons, and often five or fewer carbons. Currently, natural gas is an effective, convenient, and plentiful light hydrocarbon. As mentioned previously, various solvents or other additives can also be added to aid in extraction of hydrocarbon products from the oil shale and can often also increase fluidity.\|[0092] The light hydrocarbon can be introduced into the permeable body by conveying the same through a delivery conduit having an open end in fluid communication with a lower portion of the permeable body such that the light hydrocarbons (which are a gas under normal operating conditions) permeate up through the permeable body. Alternatively, this same approach can be applied to recovered hydrocarbons which are first delivered to an empty impoundment. In this way, the impoundment can act as a holding tank for direct products from a nearby impoundment and as a reformer or upgrader. In this embodiment, the impoundment can be at least partially filled with a liquid product where the gaseous light hydrocarbon is passed through and allowed to contact the liquid hydrocarbon products at temperatures and conditions sufficient to achieve reforming in accordance with well known processes. Optional reforming catalysts which include metals such as Pd, Ni or other suitable catalytically active metals can also be included in the liquid product within the impoundment. The addition of catalysts can serve to lower and/or adjust reforming temperature and/or pressure for particular liquid products. Further, the impoundments can be readily formed at almost any depth. Thus, optimal reforming pressures (or recovery pressures when using impoundment depth as pressure control measure for recovery from a permeable body) can be designed based on hydrostatic pressure due to the amount of liquid in the impoundment and the height of the impoundment, i.e. P=ρgh. In addition, the pressure can vary considerably over the height of the impoundment sufficient to provide multiple reforming zones and tailorable pressures. Generally, pressures within the permeable body can be sufficient to achieve substantially only liquid extraction, although some minor volumes of vapor may be produced depending on the particular composition of the permeable body. As a general guideline, pressures can range from about 5 atm to about 50 atm, although pressures from about 6 atm to about 20 atm can be particularly useful. However, any pressure greater than about atmospheric can be used.\|[0093] In one embodiment, extracted crude has fines precipitated out within the subdivided capsules. Extracted fluids and gases can be treated for the removal of fines and dust particles. Separation of fines from shale oil can be accomplished by techniques such as, but not limited to, hot gas filtering, precipitation, and heavy oil recycling.\|[0094] Hydrocarbon products recovered from the permeable body can be further processed (e.g. refined) or used as produced. Any condensable gaseous products can be condensed by cooling and collection, while non-condensable gases can be collected, burned as fuel, reinjected, or otherwise utilized or disposed of. Optionally, mobile equipment can be used to collect gases. These units can be readily oriented proximate to the control infrastructure and the gaseous product directed thereto via suitable conduits from an upper region of the control infrastructure.\|[0095] In yet another alternative embodiment, heat within the permeable body can be recovered subsequent to primary recovery of hydrocarbon materials therefrom. For example, a large amount of heat is retained in the permeable body. In one optional embodiment, the permeable body can be flooded with a heat transfer fluid such as water to form a heated fluid, e.g. heated water and/or steam. At the same time, this process can facilitate removal of some residual hydrocarbon products via a physical rinsing of the spent shale solids. In some cases, the introduction of water and presence of steam can result in water gas shift reactions and formation of synthesis gas. Steam recovered from this process can be used to drive a generator, directed to another nearby infrastructure, or otherwise used. Hydrocarbons and/or synthesis gas can be separated from the steam or heated fluid by conventional methods.\|[0096] Although the methods and infrastructure allow for improved permeability and control of operating conditions, significant quantities of unrecovered hydrocarbons, precious metals, minerals, sodium bicarbonate or other commercially valuable materials often remain in the permeable body. Therefore, a selective solvent can be injected or introduced into the permeable body. Typically, this can be done subsequent to collecting the hydrocarbons, although certain selective solvents can be beneficially used prior to heating and/or collection. This can be done using one or more of the existing conduits or by direct injection and percolation through the permeable body. The selective solvent or leachate can be chosen as a solvent for one or more target materials, e.g. minerals, precious metal, heavy metals, hydrocarbons, or sodium bicarbonate. In one specific embodiment, steam or carbon dioxide can be used as a rinse of the permeable body to dislodge at least a portion of any remaining hydrocarbons. This can be beneficial not only in removing potentially valuable secondary products, but also in cleaning remaining spent materials of trace heavy metal or inorganics to below detectable levels in order to comply with regulatory standards or to prevent inadvertent leaching of materials at a future date.\|[0097] More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body. Typically, such recovery of materials can be performed prior to heat treatment of the permeable body. Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like. For example, heavy metals, bauxite or aluminum, and mercury can be removed by flooding the permeable body with an appropriate solvent and recirculating the resulting leachate through appropriately designed ion exchange resins (e.g. beads, membranes, etc.).\|[0098] Similarly, bioextraction, bioleaching, biorecovery, or bioremediation of hydrocarbon material, spent materials, or precious metals can be performed to further improve remediation, extract valuable metals, and restoration of spent material to environmentally acceptable standards. In such bioextraction scenarios, conduits can be used to inject catalyzing gases as a precursor which helps to encourage bioreaction and growth. Such microorganisms and enzymes can biochemically oxidize the ore body or material or cellulosic or other biomass material prior to an ore solvent extraction via bio-oxidation. For example, a perforated pipe or other mechanism can be used to inject a light hydrocarbon (e.g. methane, ethane, propane or butane) into the permeable body sufficient to stimulate growth and action of native bacteria. Bacteria can be native or introduced and may grow under aerobic or anaerobic conditions. Such bacteria can release metals from the permeable body which can then be recovered via flushing with a suitable solvent or other suitable recovery methods. The recovered metals can then be precipitated out using conventional methods.\|[0099] Synthesis gas can also be recovered from the permeable body during the step of heating. Various stages of gas production can be manipulated through processes which raise or lower operating temperatures within the encapsulated volume and adjust other inputs into the impoundment to produce synthetic gases which can include but are not limited to, carbon monoxide, hydrogen, hydrogen sulfide, hydrocarbons, ammonia, water, nitrogen or various combinations thereof. In one embodiment, temperature and pressure can be controlled within the permeable body to lower CO2 emissions as synthetic gases are extracted.\|[0100] Hydrocarbon product recovered from the constructed infrastructures can most often be further processed, e.g. by upgrading, refining, etc. Sulfur from related upgrading and refining processing can be isolated in various constructed sulfur capsules within the greater structured impoundment capsule. Constructed sulfur capsules can be spent constructed infrastructures or dedicated for the purpose of storage and isolation after desulfurization.\|[0101] Similarly, spent hydrocarbonaceous material remaining in the constructed infrastructure can be utilized in the production of cement and aggregate products for use in construction or stabilization of the infrastructure itself or in the formation of offsite constructed infrastructures. Such cement products made with the spent shale may include, but are not limited to, mixtures with Portland cement, calcium salt, volcanic ash, perlite, synthetic nano carbons, sand, fiber glass, crushed glass, asphalt, tar, binding resins, cellulosic plant fibers, and the like.\|[0102] In still another embodiment, injection, monitoring and production conduits or extraction egresses can be incorporated into any pattern or placement within the constructed infrastructure. Monitoring wells and constructed geo membrane layers beneath or outside of the constructed capsule containment can be employed to monitor unwanted fluid and moisture migration outside of containment boundaries and the constructed infrastructure.\|[0103] Although a filled and prepared constructed infrastructure can often be immediately heated to recover hydrocarbons, this is not required. For example, a constructed infrastructure which is built and filled with mined hydrocarbonaceous material can be left in place as a proven reserve. Such structures are less susceptible to explosion or damage due to terrorist activity and can also provide strategic reserves of unprocessed petroleum products, with classified and known properties so that economic valuations can be increased and more predictable. Long term petroleum storage often faces quality deterioration issues over time. Thus, these approaches can optionally be used for long term quality insurance and storage with reduced concerns regarding breakdown and degradation of hydrocarbon products.\|[0104] In still another aspect, the high quality liquid product can be blended with more viscous lower quality (e.g. lower API) hydrocarbon products. For example, kerogen oil produced from the impoundments can be blended with bitumen to form a blended oil. The bitumen is typically not transportable through an extended pipeline under conventional and accepted pipeline standards and can have a viscosity substantially above and an API substantially below that of the kerogen oil. By blending the kerogen oil and bitumen, the blended oil can be rendered transportable without the use of additional diluents or other viscosity or API modifiers. As a result, the blended oil can be pumped through a pipeline without requiring additional treatments to remove a diluent or returning such diluents via a secondary pipeline. Conventionally, bitumen is combined with a diluent such as natural gas condensate or other low molecular weight liquids, to allow pumping to a remote location. The diluent is removed and returned via a second pipeline back to the bitumen source. These approaches allow for elimination of returning diluent and simultaneous upgrading of the bitumen.\|[0105] Difficult problems can thus be solved related to the extraction of hydrocarbon liquids and gases from surface or underground mined hydrocarbon bearing deposits such as oil shale, tar sands, lignite, and coal, and from harvested biomass. Among other things, these methods and systems help reduce cost, increase volume output, lower air emissions, limit water consumption, prevent underground aquifer contamination, reclaim surface disturbances, reduce material handling costs, remove dirty fine particulates, and improve composition of recovered hydrocarbon liquid or gas. Water contamination issues can also be addressed with a safer, more predictable, engineered, observable, repairable, adaptable and preventable water protection structure.\|[0106] Although the described methods and systems are mining-dependent, they are not limited or encumbered to conventional aboveground (ex-situ) retorting processes. This approach improves upon the benefits of surface retorts including better process control of temperature, pressure, injection rates, fluid and gas compositions, product quality and better permeability due to processing and heating mined rubble. These advantages are available while still addressing the volume, handling, and scalability issues most fabricated surface retorts cannot provide.\|[0107] Other improvements which can be realized are related to environmental protection. Conventional surface retorts have had the problem of spent shale after it has been mined and has passed through a surface retort. Spent shale which has been thermally altered requires special handling to reclaim and isolate from surface drainage basins and underground aquifers. These methods and systems can address reclamation and retorting in a uniquely combined approach. In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants.\|[0108] It is to be understood that the above-referenced arrangements are illustrative of the application for the principles of the present invention. Thus, while the present invention has been described above in connection with the exemplary embodiments, it will be apparent to those of ordinary skill in the art that numerous modifications and alternative arrangements can be made without departing from the principles and concepts of the invention as set forth in the claims.	Family Number\|(35298)\|35298\|Title\|(AU2010213862 B2)\|Carbon management and sequestration from encapsulated control infrastructures\|(AU2010213862 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(CA2752524 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(CN102395657 A)\|Carbon management and sequestration from encapsulated control infrastructures \|(EA201171023 A1)\|Carbon monitoring and sequestration from sealed controlled infrastructures\|(EP2406353 A4)\|Carbon management and sequestration from encapsulated control infrastructures\|(EP2406353 A2)\|Carbon management and sequestration from encapsulated control infrastructures\|(IL-214555 A)\|Carbon management and sequestration from encapsulated control infrastructures\|(MA--33117 B1)\|Carbon management and sequestration from encapsulated control infrastructures\|(MX2011008525 A)\|Carbon management and sequestration from encapsulated control infrastructures\|Carbon management and sequestration from encapsulated control infrastructures.\|(MX-319678 B)\|Carbon management and sequestration from encapsulated control infrastructure.\|(US8323481 B2)\|Carbon management and sequestration from encapsulated control infrastructures\|(US20100200465 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(WO201093684 A3)\|Carbon management and sequestration from encapsulated control infrastructures\|(WO201093684 A2)\|Carbon management and sequestration from encapsulated control infrastructures\|(IN2011MN01897 A)\|Carbon management and sequestration from encapsulated control infrastructures\|(EG--26451 A)\|Carbon management and sequestration from encapsulated control infrastructures\|(MY-152266 A)\|Carbon management and sequestration form encapsulated control infrastructures\|(TN2011000396 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(BR201008447 A2)\|Carbon management and sequestration from encapsulated control infrastructures\|(ZA201106558 B)\|Carbon management and sequestration from encapsulated control infrastructures\|(PE201200704 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(AP2011005878 A0)\|Carbon management and sequestration from encapsulated control infrastructures\|Carbon management and sequestration from encapsulated control infrastructures.\|(GE201406167 B)\|Carbon management and sequestration from encapsulated control infrastructures\|(VE2010000234 A)\|Carbon management and sequestration from encapsulated control infrastructure.\|Advantages / Prev. Drawbacks\|(CN102395657 A)\|Other methods include in situ radio frequency methods ( microwaves ) and " modified " in situ processes where underground mining , blasting and retorting have been used in combination to produce crushed rock from a formation to allow for better heat transfer and product removal . \|	Basic materials chemistry\|Civil 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KR100595792; KR10-0595792\|\|JP2000317302; CN101125651; CN1956768; US20080190815; KR100595792\|\|\|\|\|\|\|US4133580; US4423907; US4424021; US4717146; US4984594; US6841077; US6991033; US20070000662; US20090000744; US7862705; US7862706; US4430195; US5868202; US6854929; US7004247; US7004251; US7004678; US20070023186; US3652447; US4502920; US5190405; US5193934; US4017119; US4151068; US4440446; US6051137; US6543535; US6543539; US6875356; US6881009; US7032660; US3661423; US3954140; US4155967; US4266612; US4266826; US4449586; US5114497; US6732796; US7040397; US7040399; US7048051; US7051811; US7534926; US4029571; US4096912; US4158622; US4452689; US4454915; US5024487; US5221827; US5318116; US6902138; US7066254; US20110138649; US1919636; US4851134; US5229583; US6419423; US6918443; US7070758; US7073578; US7077198; US7077199; US4043595; US4106814; US4219237; US5041209; US5137539; US5340467; US5543041; US5656239; US5660500; US6102622; US6110359; US6923257; US6929330; US7090013; US7091460; US20080190813; US20080190816; US20080190818; US20080192815; US20100200467; US2481051; US4221648; US5244310; US5553189; US5948253; US20060213657; US3910834; US4294563; US4353418; US5674424; US6632047; US20040211569; US6951247; US3919390; US4199327; US5139535; US1919636; US2481051; US3617471; US3652447; US3661423; US3910834; US3954140; US4017119; US4029571; US4043595; US4096912; US4106814; US4133580; US4151068; US4155967; US4158622; US4171146; US4219237; US4221648; US4234230; US4241952; US4266612; US4266826; US4294563; US4303533; US4353418; US4376107; US4415365; US4423907; US4424021; US4430195; US4440446; US4449586; US4452689; US4454915; US4502920; US4851134; US4879019; US4984594; US5024487; US5041209; US5076727; US5114497; US5137539; US5190405; US5193934; US5221827; US5229583; US5244310; US5271693; US5318116; US5340467; US5372621; US5372708; US5478443; US5543041; US5553189; US5656239; US5660500; US5674424; US5843214; US5868202; US5948253; US5997214; US6051137; US6102622; US6110359; US6419423; US6485232; US6543535; US6543539; US6632047; US6732796; US6811683; US6824328; US6841077; US6854929; US6875356; US6881009; US6902138; US6918443; US6923257; US6929330; US6951247; US6962466; US6991033; US7004247; US7004251; US7004678; US7032660; US7040397; US7040399; US7048051; US7051811; US7066254; US7070758; US7073578; US7077198; US7077199; US7090013; US7091460; US7114566; US7121342; US7534926; US7862705; US7862706; KR10-0595792; JP2005306721; JP2009090168; US20040211569; US20060213657; US20070000662; US20070023186; US20080077430; US20080190813; US20080190815; US20080190816; US20080190818; US20090007484; US20090250380; US20100200467; US20110138649	(EP2406353)\|Search Report references [Examiner]\|-See also references of WO 2010093684A2\|\|(US8323481)\|Applicant references\|-U.S. Appl. No. 12/703,560, filed Feb. 10, 2010; Todd Dana; Office action issued Nov. 18, 2011.\|-U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana; notice of allowance issued Oct. 26, 2011.\|-Alternative Methods for Fluid Delivery and Recovery; Manual; Sep. 1994; United States Environmental Protection Agency; 87 pgs.\|-U.S. Appl. No. 12/703,638, filed Feb. 10, 2010, Todd Dana.\|-U.S. Appl. No. 12/704,440, filed Feb. 11, 2010, Todd Dana.\|-U.S. Appl. No. 12/702,899, filed Feb. 9, 2010, Todd Dana.\|-U.S. Appl. No. 12/703,560, filed Feb. 10, 2010, Todd Dana.\|-U.S. Appl. No. 12/704,596, filed Feb. 12, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,073, filed Feb. 5, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,141, filed Feb. 5, 2010, Todd Dana.\|-PCT Application PCT/US2010/058948; filed Dec. 3, 2010; James W. Patten; International Search Report mailed Aug. 31, 2011.\|-PCT Application PCT/US2010/060854; filed Dec. 16, 2010; James W. Patten; International Search Report mailed Aug. 26, 2011.\|-Slow Sand Filter: http://en.wikipedia.org/wiki/Slow-sand-filter; Nov. 9, 2009; 4 pages.\|-Sand Filter: http://en.wikipedia.org/wiki/Sand-filter; Nov. 9, 2009; 6 pages.\|-RELATED CASE: U.S. Appl. No. 12/960,215, filed Dec. 3, 2010; James Patten.\|-RELATED CASE: U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana.\|-U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana; office action issued Jun. 1, 2011.\|-PCT Application PCT/US2010/023740; filed Feb. 10, 2010; Todd Dana; ISR issued Sep. 16, 2010.\|-U.S. Appl. No. 12/703,560, filed Feb. 10, 2010; Todd Dana; office action issued Apr. 24, 2012.\|-U.S. Appl. No. 12/703,560, filed Feb. 10, 2010; Todd Dana; notice of allowance dated Sep. 4, 2012.\|\|(WO2010/093684)\|International Search Report [Examiner]\|-See also references of EP 2406353A2\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|	GRANTED	(EP2406353)\|LAPSED\|(US8323481)\|LAPSED\|(WO2010/093684)\|LAPSED\|(CN102395657)\|LAPSED\|(GEP20146167)\|GRANTED\|(MY152266)\|GRANTED\|(MX319678)\|GRANTED\|(UA104616)\|GRANTED\|(EG26451)\|GRANTED\|(AU2010213862)\|EXPIRED\|(ZA201106558)\|GRANTED\|(MA33117)\|GRANTED\|(BRPI1008447)\|LAPSED\|(TN2011000396)\|PENDING\|(VE2010000234)\|LAPSED\|(PE20120704)\|REVOKED\|(EA201171023)\|LAPSED\|(IN1897/MUMNP/2011)\|LAPSED\|(AP2011005878)\|LAPSED\|(IL214555)\|LAPSED\|(CA2752524)\|LAPSED	ALIVE	(EP2406353)\|DEAD\|(US8323481)\|DEAD\|(WO2010/093684)\|DEAD\|(CN102395657)\|DEAD\|(GEP20146167)\|ALIVE\|(MY152266)\|ALIVE\|(MX319678)\|ALIVE\|(UA104616)\|ALIVE\|(EG26451)\|ALIVE\|(AU2010213862)\|DEAD\|(ZA201106558)\|ALIVE\|(MA33117)\|ALIVE\|(BRPI1008447)\|DEAD\|(TN2011000396)\|ALIVE\|(VE2010000234)\|DEAD\|(PE20120704)\|DEAD\|(EA201171023)\|DEAD\|(IN1897/MUMNP/2011)\|DEAD\|(AP2011005878)\|DEAD\|(IL214555)\|DEAD\|(CA2752524)\|DEAD	(EP2406353)\|LEGAL DETAILS FOR EP2406353\|Actual or expected expiration date=2015-03-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP10741655\|Application date=2010-02-10\|Standardized application number=2010EP-0741655\|Event publication date=2011-12-16\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2012-01-18\|Event code=EP/A2\|Event group=Examination events\|Application published without search report\|Publication country=EP\|Publication number=EP2406353\|Publication stage code=A2\|Publication date=2012-01-18\|Standardized publication number=EP2406353\|Event publication date=2012-01-18\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2011-09-12\|Event publication date=2012-01-18\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR\|Event publication date=2012-05-16\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2014-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP2406353\|Publication stage code=A4\|Publication date=2014-09-17\|Standardized publication number=EP2406353\|Event publication date=2014-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2014-08-21\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2015-09-18\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2015-10-21\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2015-03-20\|(US8323481)\|LEGAL DETAILS FOR US8323481\|Actual or expected expiration date=2025-01-06\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-05\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US12701156\|Application date=2010-02-05\|Standardized application number=2010US-12701156\|Event publication date=2010-02-05\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:MCCAIG, BRIAN A\|Event publication date=2010-02-05\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1774\|Event publication date=2010-02-05\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 2488-025.NP\|Event publication date=2010-02-05\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 20551\|Event publication date=2010-02-05\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2010-02-05\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2010-02-26\|Event code=US/INCD\|Event group=Examination events OAO\|Notice Mailed--Application Incomplete--Filing Date Assigned\|Event publication date=2010-02-26\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2010-03-11\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DANA, TODD;PATTEN, JAMES W.;SIGNING DATES FROM 20090511 TO 20090623\|Reel/frame:024064/0164\|OWNER:RED LEAF RESOURCES, INC., UTAH\|Event publication date=2010-03-17\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|SECURITY AGREEMENT\|Assignors:RED LEAF RESOURCES, INC., DBA ECOSHALE AND ECOSHALE ENERGY;RED LEAF HOLDINGS, LLC;NATIONS MINING, LLC;AND OTHERS\|Reel/frame:024097/0397\|OWNER:CARDINAL ENERGY HOLDINGS, LLC, UTAH\|Effective date of the event=2009-07-02\|Event publication date=2010-04-12\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DANA, TODD;PATTEN, JAMES W.;SIGNING DATES FROM 20100317 TO 20100324\|Reel/frame:024215/0959\|OWNER:RED LEAF RESOURCES, INC., UTAH\|Event publication date=2010-04-26\|Event code=US/FLFEE\|Event group=Payment or non-payment notifications\|Payment of additional filing fee/Preexam\|Event publication date=2010-05-06\|Event code=US/POAC\|Event group=Change of name or address\|Change in Power of Attorney (May Include Associate POA)\|Event publication date=2010-05-06\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2010-05-10\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|RELEASE BY SECURED PARTY\|Assignor:CARDINAL ENERGY HOLDINGS, LLC.\|Reel/frame:024357/0626\|OWNER:RED LEAF RESOURCES, INC., D/B/A ECOSHALE, ECHOSHAL\|Effective date of the event=2010-05-07\|Event publication date=2010-05-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2010-08-12\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20100200465\|Publication stage code=A1\|Publication date=2010-08-12\|Standardized publication number=US20100200465\|Event publication date=2010-08-12\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2011-01-15\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-01-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-05-23\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-06-28\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-10-28\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-11-21\|Event code=US/RESTREQ\|Event group=Examination events Corrections OAO\|Restriction/Election Requirement\|Event publication date=2011-12-14\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-01-03\|Event code=US/ELC\|Event group=Examination events OAI\|Response to Election / Restriction Filed\|Event publication date=2012-03-07\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2012-03-12\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2012-03-12\|R4R=103a\|RJST=non-final\|Rejected claims 1 and 11-13; 1 and 11-12\|RJCT=US5139535\|RJCT=US4199327\|Event publication date=2012-06-11\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2012-07-23\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-07-25\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2012-07-29\|Event code=US/ZAAA\|Event group=Administrative notifications Payment or non-payment notifications\|NOTICE OF ALLOWANCE AND FEES DUE\|Original code: NOA\|Event publication date=2012-07-30\|Event code=US/ZAAB\|Event group=Administrative notifications Examination events\|NOTICE OF ALLOWANCE MAILED\|Original code: MN/=.\|Event publication date=2012-07-30\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2012-09-20\|Event code=US/M327\|Event group=Examination events OAO\|Miscellaneous Communication to Applicant - No Action Count\|Event publication date=2012-10-12\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-10-19\|Event code=US/M327\|Event group=Examination events OAO\|Miscellaneous Communication to Applicant - No Action Count\|Event publication date=2012-10-30\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2012-10-30\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2012-11-02\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2012-11-14\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2012-12-04\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US08323481\|Publication stage code=B2\|Publication date=2012-12-04\|Standardized publication number=US8323481\|Event publication date=2012-12-04\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 240 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 71 Adjustment total: \|Number of days of extension=169\|Event publication date=2015-12-15\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2016-05-16\|Event code=US/FPAY\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Fee payment recorded\|Annual fees payment date=2016-05-16\|Year of payment of annual fees=4\|Event publication date=2019-12-17\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|Event publication date=2020-04-07\|Event code=US/MAFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|Maintenance Fee Payment\|Annual fees payment date=2020-04-07\|Year of payment of annual fees=8\|PAYMENT OF MAINTENANCE FEE, 8TH YR, SMALL ENTITY (ORIGINAL EVENT CODE: M2552)\|Entity status of patent owner: SMALL ENTITY\|Event publication date=2020-04-07\|Event code=US/M2552\|Event group=Payment or non-payment notifications\|Payment of Maintenance Fee, 8th Yr, Small Entity\|Event publication date=2023-12-19\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=11\|Event publication date=2024-07-22\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2024-12-04\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2024-12-04\|Event publication date=2025-01-06\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2025-01-06\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|(WO2010/093684)\|LEGAL DETAILS FOR WO2010/093684\|Actual or expected expiration date=2012-08-12\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2010023740\|Application date=2010-02-10\|Standardized application number=2010WO-US23740\|Event publication date=2010-08-19\|Event code=WO/A2\|Event group=Examination events\|International application published with declaration under Article 17 (2) (a)\|Publication country=WO\|Publication number=WO2010093684\|Publication stage code=A2\|Publication date=2010-08-19\|Standardized publication number=WO201093684\|Event publication date=2010-11-18\|Event code=WO/A3\|Event indicator=Pos\|Event group=Examination events\|Later publication of ISR with revised front page\|Publication country=WO\|Publication number=WO2010093684\|Publication stage code=A3\|Publication date=2010-11-18\|Standardized publication number=WO201093684\|Event publication date=2012-08-12\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AP2011005878\|Actual or expected expiration date=2016-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=AP Corresponding appl: AP2011005878\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2011AP-0005878\|Corresponding cc:\|Designated or member state=AP Corresponding pat: AP2011005878\|Publication stage code in the designated or member state=A0\|Publication date in the 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state=2010-02-10\|Application number in the designated or member state=2010CA-2752524\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA2752524\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2010-08-19\|Publication number in the designated or member state=CA2752524\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CA\|Event publication date=2016-03-23\|Event code=CA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR CL\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=CL Corresponding appl: CL2011001962\|Event publication date=2011-08-11\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CL\|MEMBER STATE LEGAL DETAILS FOR CN102395657\|Actual or expected expiration date=2015-01-14\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN201080016478\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2010CN-80016478\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN102395657\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-03-28\|Publication number in the designated or member state=CN102395657\|Event publication date=2010-02-10\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CN\|Event publication date=2015-01-14\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2011-08-12\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2011-08-12\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR DZ\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=DZ Corresponding appl: DZDZP2011000597\|Event publication date=2011-09-08\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=DZ\|MEMBER STATE LEGAL DETAILS FOR EA201171023\|Actual or expected expiration date=2017-03-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EA Corresponding appl: EA201171023\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2011EA-0071023\|Corresponding cc:\|Designated or member state=EA Corresponding pat: EA201171023\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2012-03-30\|Publication number in the designated or member state=EA201171023\|Event publication date=2011-09-08\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EA\|Event publication date=2012-03-30\|Event code=EA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EA\|MEMBER STATE LEGAL DETAILS FOR EG26451\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=EG Corresponding appl: EG2011081359\|Application date in the designated or member state=2011-08-11\|Application number in the designated or member state=2011EG-0081359\|Corresponding cc:\|Designated or member state=EG Corresponding pat: EG26451\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2013-11-12\|Publication number in the designated or member state=EG--26451\|Event publication date=2013-11-12\|Event code=EG/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EG\|MEMBER STATE LEGAL DETAILS FOR EP2406353\|Actual or expected expiration date=2015-03-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP10741655\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2010EP-0741655\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2406353\|Publication stage code in the designated or member state=A2\|Publication date in the designated or member state=2012-01-18\|Publication number in the designated or member state=EP2406353\|Event publication date=2010-10-06\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2011-09-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2015-10-21\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR GE\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=GE Corresponding appl: GE12380\|Event publication date=2011-09-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=GE\|MEMBER STATE LEGAL DETAILS FOR IL214555\|Actual or expected expiration date=2016-09-27\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IL Corresponding appl: IL214555\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2010IL-0214555\|Corresponding cc:\|Designated or member state=IL Corresponding pat: IL214555\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-09-27\|Publication number in the designated or member state=IL-214555\|Event publication date=2011-08-09\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IL\|Event publication date=2011-09-27\|Event code=IL/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IL\|MEMBER STATE LEGAL DETAILS FOR IN1897/MUMNP/2011\|Actual or expected expiration date=2022-02-03\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN1897/MUMNP/2011\|Application date in the designated or member state=2011-09-10\|Application number in the designated or member state=2011IN-MN01897\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN1897/MUMNP/2011\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-02-03\|Publication number in the designated or member state=IN2011MN01897\|Event publication date=2011-09-10\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|Event publication date=2012-02-03\|Event code=IN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IN\|MEMBER STATE LEGAL DETAILS FOR MA33117\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=MA Corresponding appl: MA34162\|Application date in the designated or member state=2011-09-09\|Application number in the designated or member state=2011MA-0034162\|Corresponding cc:\|Designated or member state=MA Corresponding pat: MA33117\|Publication stage code in the designated or member state=B1\|Publication date in the designated or member state=2012-03-01\|Publication number in the designated or member state=MA--33117\|Event publication date=2012-03-01\|Event code=MA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=MA\|MEMBER STATE LEGAL DETAILS FOR MX2011008525\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=MX Corresponding appl: MX2011008525\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2011MX-0008525\|Corresponding cc:\|Designated or member state=MX Corresponding pat: MX2011008525\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-12-16\|Publication number in the designated or member state=MX2011008525\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=MX\|Event publication date=2014-04-24\|Event code=MX/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=MX\|MEMBER STATE LEGAL DETAILS FOR PE\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=PE Corresponding appl: PE001483-2011\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=PE\|MEMBER STATE LEGAL DETAILS FOR TN2011000396\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=TN Corresponding appl: TN2011000396\|Application date in the designated or member state=2011-08-09\|Application number in the designated or member state=2011TN-0000396\|Corresponding cc:\|Designated or member state=TN Corresponding pat: TN2011000396\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2013-03-27\|Publication number in the designated or member state=TN2011000396\|MEMBER STATE LEGAL DETAILS FOR UA104616\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=UA Corresponding appl: UAA201110768\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2011UA-0010768\|Corresponding cc:\|Designated or member state=UA Corresponding pat: UA104616\|Publication stage code in the designated or member state=C2\|Publication date in the designated or member state=2014-02-25\|Publication number in the designated or member state=UA-104616\|Event publication date=2014-02-25\|Event code=UA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=UA\|MEMBER STATE LEGAL DETAILS FOR ZA201106558\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=ZA Corresponding appl: ZA201106558\|Application date in the designated or member state=2011-09-07\|Application number in the designated or member state=2011ZA-0006558\|Corresponding cc:\|Designated or member state=ZA Corresponding pat: ZA201106558\|Publication stage code in the designated or member state=B\|Publication date in the designated or member state=2013-02-27\|Publication number in the designated or member state=ZA201106558\|Event publication date=2013-02-27\|Event code=ZA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=ZA\|(CN102395657)\|LEGAL DETAILS FOR CN102395657\|Actual or expected expiration date=2015-01-14\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201080016478\|Application date=2010-02-10\|Standardized application number=2010CN-80016478\|Event publication date=2012-03-28\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN102395657\|Publication stage code=A\|Publication date=2012-03-28\|Standardized publication number=CN102395657\|Event publication date=2012-03-28\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2012-05-09\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2015-01-14\|Event code=CN/WD01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent application deemed withdrawn after publication\|(GEP20146167)\|LEGAL DETAILS FOR GEP20146167\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-10\|Event code=GE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=GE GEAP2010012380\|Application date=2010-02-10\|Standardized application number=2010GE-0012380\|Event publication date=2014-09-25\|Event code=GE/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent for invention ( 2nd pub.)\|Publication country=GE\|Publication number=GEP20146167\|Publication stage code=B\|Publication date=2014-09-25\|Standardized publication number=GE201406167\|(MY152266)\|LEGAL DETAILS FOR MY152266\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-10\|Event code=MY/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MY MYPI2011003742\|Application date=2010-02-10\|Standardized application number=2011MY-0003742\|Event publication date=2014-09-15\|Event code=MY/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent / Utility Model\|Publication country=MY\|Publication number=MY152266\|Publication stage code=A\|Publication date=2014-09-15\|Standardized publication number=MY-152266\|(MX319678)\|LEGAL DETAILS FOR MX319678\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-10\|Event code=MX/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MX MX2011008525\|Application date=2010-02-10\|Standardized application number=2011MX-0008525\|Event publication date=2011-12-16\|Event code=MX/A\|Event group=Examination events\|Patent application\|Publication country=MX\|Publication number=MX2011008525\|Publication stage code=A\|Publication date=2011-12-16\|Standardized publication number=MX2011008525\|Event publication date=2014-04-24\|Event code=MX/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent/ granted utility model\|Publication country=MX\|Publication number=MX319678\|Publication stage code=B\|Publication date=2014-04-24\|Standardized publication number=MX-319678\|Event publication date=2014-04-24\|Event code=MX/FG\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant or registration\|Concesion\|(UA104616)\|LEGAL DETAILS FOR UA104616\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-10\|Event code=UA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=UA UAA201110768\|Application date=2010-02-10\|Standardized application number=2011UA-0010768\|Event publication date=2014-02-25\|Event code=UA/C2\|Event indicator=Pos\|Event group=Event indicating In Force\|Pat. grant. upon the USSR appl.,for which no pos. dec. made;grant. upon basis of national application\|Publication country=UA\|Publication number=UA104616\|Publication stage code=C2\|Publication date=2014-02-25\|Standardized publication number=UA-104616\|(EG26451)\|LEGAL DETAILS FOR EG26451\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-08-11\|Event code=EG/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EG EG2011081359\|Application date=2011-08-11\|Standardized application number=2011EG-0081359\|Event publication date=2013-11-12\|Event code=EG/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent for invention / Patent of addition\|Publication country=EG\|Publication number=EG26451\|Publication stage code=A\|Publication date=2013-11-12\|Standardized publication number=EG--26451\|(AU2010213862)\|LEGAL DETAILS FOR AU2010213862\|Actual or expected expiration date=2015-09-03\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=2010-02-10\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2010213862\|Application date=2010-02-10\|Standardized application number=2010AU-0213862\|Event publication date=2011-09-22\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2010213862\|Publication stage code=A1\|Publication date=2011-09-22\|Standardized publication number=AU2010213862\|Event publication date=2013-05-02\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent proceeded by OPI\|Publication country=AU\|Publication number=AU2010213862\|Publication stage code=B2\|Publication date=2013-05-02\|Standardized publication number=AU2010213862\|Event publication date=2013-08-29\|Event code=AU/FGA\|Event indicator=Pos\|Event group=Event indicating In Force\|Letters patent sealed or granted (standard patent)\|Event publication date=2015-09-03\|Event code=AU/MK14\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent ceased section 143(a) (annual fees not paid) or expired\|(ZA201106558)\|LEGAL DETAILS FOR ZA201106558\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-09-07\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA201106558\|Application date=2011-09-07\|Standardized application number=2011ZA-0006558\|Event publication date=2013-02-27\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA201106558\|Publication stage code=B\|Publication date=2013-02-27\|Standardized publication number=ZA201106558\|(MA33117)\|LEGAL DETAILS FOR MA33117\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-09-09\|Event code=MA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MA MA34162\|Application date=2011-09-09\|Standardized application number=2011MA-0034162\|Event publication date=2012-03-01\|Event code=MA/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=MA\|Publication number=MA33117\|Publication stage code=B1\|Publication date=2012-03-01\|Standardized publication number=MA--33117\|(BRPI1008447)\|LEGAL DETAILS FOR BRPI1008447\|Actual or expected expiration date=2019-10-01\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=BR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=BR BRPI1008447\|Application date=2010-02-10\|Standardized application number=2010BR-0008447\|Event publication date=2019-09-24\|Event code=BR/A2\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention / pipeline patent published without search report\|Publication country=BR\|Publication number=BRPI1008447\|Publication stage code=A2\|Publication date=2019-09-24\|Standardized publication number=BR201008447\|Event publication date=2019-10-01\|Event code=BR/B08F\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application fees: dismissal - article 86 of industrial property law\|Anuidade do pedido: arquivamento . Art. 86 da lpi [codigo 8.6 rpi]\|Event publication date=2020-01-21\|Event code=BR/B08K\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Lapse as no evidence of payment of the annual fee has been furnished to inpi (acc. art. 87)\|Manutencao do arquivamento [codigo 8.11 rpi]\|EM VIRTUDE DO ARQUIVAMENTO PUBLICADO NA RPI 2543 DE 01-10-2019 E CONSIDERANDO AUSENCIA DE MANIFESTACAO DENTRO DOS PRAZOS LEGAIS, INFORMO QUE CABE SER MANTIDO O ARQUIVAMENTO DO PEDIDO DE PATENTE, CONFORME O DISPOSTO NO ARTIGO 12, DA RESOLUCAO 113/2013.\|(TN2011000396)\|LEGAL DETAILS FOR TN2011000396\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2011-08-09\|Event code=TN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=TN TN2011000396\|Application date=2011-08-09\|Standardized application number=2011TN-0000396\|Event publication date=2013-03-27\|Event code=TN/A1\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention\|Publication country=TN\|Publication number=TN2011000396\|Publication stage code=A1\|Publication date=2013-03-27\|Standardized publication number=TN2011000396\|(VE2010000234)\|LEGAL DETAILS FOR VE2010000234\|Actual or expected expiration date=2017-07-26\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-12\|Event code=VE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=VE VE2010-000234\|Application date=2010-02-12\|Standardized application number=2010VE-0000234\|Event publication date=2012-07-26\|Event code=VE/A\|Event indicator=Pos\|Event group=Examination events\|Patent Application or Foreign Patent Application\|Publication country=VE\|Publication number=VE2010000234\|Publication stage code=A\|Publication date=2012-07-26\|Standardized publication number=VE2010000234\|Event publication date=2017-07-26\|Event code=VE/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(PE20120704)\|LEGAL DETAILS FOR PE20120704\|Actual or expected expiration date=2016-05-30\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2010-02-10\|Event code=PE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=PE PE2011001483\|Application date=2010-02-10\|Standardized application number=2011PE-0001483\|Event publication date=2012-06-27\|Event code=PE/A1\|Event group=Examination events\|Patent application\|Publication country=PE\|Publication number=PE20120704\|Publication stage code=A1\|Publication date=2012-06-27\|Standardized publication number=PE201200704\|Event publication date=2016-05-30\|Event code=PE/FC\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Refusal\|Rechazada o denegada\|(EA201171023)\|LEGAL DETAILS FOR EA201171023\|Actual or expected expiration date=2017-03-30\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=EA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EA EA201171023\|Application date=2010-02-10\|Standardized application number=2011EA-0071023\|Event publication date=2012-03-30\|Event code=EA/A1\|Event group=Examination events\|Public. of applic. with search report\|Publication country=EA\|Publication number=EA201171023\|Publication stage code=A1\|Publication date=2012-03-30\|Standardized publication number=EA201171023\|Event publication date=2017-03-30\|Event code=EA/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IN1897/MUMNP/2011)\|LEGAL DETAILS FOR IN1897/MUMNP/2011\|Actual or expected expiration date=2022-02-03\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-09-10\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN1897/MUMNP/2011\|Application date=2011-09-10\|Standardized application number=2011IN-MN01897\|Event publication date=2012-02-03\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN1897/MUMNP/2011\|Publication stage code=A\|Publication date=2012-02-03\|Standardized publication number=IN2011MN01897\|Event publication date=2022-02-03\|Event code=IN/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(AP2011005878)\|LEGAL DETAILS FOR AP2011005878\|Actual or expected expiration date=2016-10-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=AP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AP AP2011005878\|Application date=2010-02-10\|Standardized application number=2011AP-0005878\|Event publication date=2011-10-31\|Event code=AP/A0\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=AP\|Publication number=AP2011005878\|Publication stage code=A0\|Publication date=2011-10-31\|Standardized publication number=AP2011005878\|Event publication date=2016-10-31\|Event code=AP/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IL214555)\|LEGAL DETAILS FOR IL214555\|Actual or expected expiration date=2016-09-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=IL/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IL IL214555\|Application date=2010-02-10\|Standardized application number=2010IL-0214555\|Event publication date=2011-09-27\|Event code=IL/A\|Event group=Examination events\|Application of patent for invention\|Publication country=IL\|Publication number=IL214555\|Publication stage code=A\|Publication date=2011-09-27\|Standardized publication number=IL-214555\|Event publication date=2016-09-27\|Event code=IL/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(CA2752524)\|LEGAL DETAILS FOR CA2752524\|Actual or expected expiration date=2016-02-10\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2752524\|Application date=2010-02-10\|Standardized application number=2010CA-2752524\|Event publication date=2010-08-19\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2752524\|Publication stage code=A1\|Publication date=2010-08-19\|Standardized publication number=CA2752524\|Event publication date=2016-03-23\|Event code=CA/FZDE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Dead\|Effective date of the event=2016-02-10	(EP2406353)\|Contracting States: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2010/093684)\|ARIPO: GH, GM, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2010/093684)\|EAPO: RU, TJ, BY, MD, AZ, TM, AM, KG, KZ\|(WO2010/093684)\|EPO: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2010/093684)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2010/093684)\|National States: PT, HN, HR, HU, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KM, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PE, PG, PH, PL	(WO2010/093684)\|CL; DZ; EG; GE; MA; MX; PE; TN; UA; ZA\|(GEP20146167)\|GE\|(MY152266)\|MY\|(MX319678)\|MX\|(UA104616)\|UA\|(EG26451)\|EG\|(ZA201106558)\|ZA\|(MA33117)\|MA\|(TN2011000396)\|TN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=jP3Nqvhw8TidMHrg3/9433mXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US8323481&ekey=935&xpn=EP2406353&kind=A4	https://register.epo.org/application?number=EP10741655	https://permalink.orbit.com/RenderStaticFirstPage?XPN=xq6OlXDbYJOeccOAsqvWAnfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2010/093684)\|US\|(US8323481)\|US	(WO2010/093684)\|NAME=RED LEAF RESOURCES, INC. 200 W. Civic Center Drive, Suite 190, Sandy, UT 84070 , COUNTRY=US\|(US8323481)\|NAME=Red Leaf Resources, Inc. , CITY=Sandy , STATE=UT , COUNTRY=US , ATYP=US Company	(EP2406353)\|DE\|(EP2406353)\|DE\|\|(US20100200465)\|US\|(WO2010/093684)\|US\|\|\|\|(AU2010213862)\|AU\|(AU2010213862)\|AU\|\|(CA2752524)\|CA	(EP2406353)\|NAME=Walker, Ross Thomson;Forresters Skygarden Erika-Mann-Strasse 11 , CITY=80636 München , COUNTRY=DE , REG=101298687\|(EP2406353)\|NAME=Walker, Ross Thomson;Forrester & Boehmert Pettenkoferstrasse 20-22 , CITY=80336 München , COUNTRY=DE , REG=100045009\|(US8323481)\|NAME=Thorpe North & Western LLP\|(US20100200465)\|NAME=THORPE NORTH & WESTERN, LLP. P.O. Box 1219 , CITY=SANDY , STATE=UT , POSTCODE=84091-1219 , COUNTRY=US\|(WO2010/093684)\|NAME=ERICKSEN, Erik S. et al. THORPE NORTH & WESTERN, LLP, P.O. Box 1219, Sandy, UT 84091-1219 , COUNTRY=US\|(CN102395657)\|NAME=ZHAO RONGMIN;JEEKAI & PARTNERS , REG=11245\|(MX319678)\|NAME=MARIA ANGELICA PARDAVELL JUAREZ\|(MX2011008525)\|NAME=MARIA ANGELICA PARDAVELL JUAREZ\|(AU2010213862)\|NAME=FB Rice Level 23 44 Market Street , CITY=SYDNEY , STATE=NSW , POSTCODE=2000 , COUNTRY=AU\|(AU2010213862)\|NAME=FB Rice Level 23 44 Market Street , CITY=Sydney , STATE=NSW , POSTCODE=2000 , COUNTRY=AU\|(VE2010000234)\|NAME=LINARES ALLOCA MARLIN ENEIDA\|(CA2752524)\|NAME=BERESKIN & PARR LLP/S.E.N.C.R.L.,S.R.L. , COUNTRY=CA	(EP2406353)\|US; US\|(EP2406353)\|US; US\|(US8323481)\|US; US\|(US20100200465)\|US; US\|\|(WO2010/093684)\|US; US\|\|\|\|(MX319678)\|US; US\|\|\|\|\|\|\|\|\|\|\|\|(IN1897/MUMNP/2011)\|US; US\|\|(CA2752524)\|US; US	(EP2406353)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, CITY=Park CityUT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., CITY=SandyUT 84092, COUNTRY=US\|(EP2406353)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, CITY=Park CityUT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., CITY=SandyUT 84092, COUNTRY=US\|(US8323481)\|NAME=Dana Todd, CITY=Park City, STATE=UT , COUNTRY=US \|NAME=Patten James W., CITY=Sandy, STATE=UT , COUNTRY=US\|(US20100200465)\|NAME=Dana Todd, CITY=Park City, STATE=UT , COUNTRY=US \|NAME=Patten James W., CITY=Sandy, STATE=UT , COUNTRY=US\|(WO2010/093684)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(WO2010/093684)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, Park City, UT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., Sandy, UT 84092, COUNTRY=US\|(CN102395657)\|NAME=DANA TODD\|NAME=PATTEN JAMES W.\|(GEP20146167)\|NAME=DANA, Todd\|NAME=PATTEN, James, W.\|(MY152266)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES W.\|(MX319678)\|NAME=TODD DANA, COUNTRY=US \|NAME=JAMES W PATTEN, COUNTRY=US\|(MX2011008525)\|NAME=TODD DANA\|NAME=JAMES W PATTEN\|(UA104616)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(EG26451)\|NAME=DANA TODD 3473 W. Daybreaker Drive Park City, UT 84098 (US)\|NAME=PATTEN JAMES W 4216 E. Wildcreek Rd. Sandy, UT 84092 (US)\|(AU2010213862)\|NAME=Dana, Todd\|NAME=Patten, James W.\|(AU2010213862)\|NAME=Dana, Todd\|NAME=Patten, James W.\|(ZA201106558)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(MA33117)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(BRPI1008447)\|NAME=James W. Patten\|NAME=Todd Dana\|(TN2011000396)\|NAME=PATTEN JAMES W.\|NAME=DANA TODD\|(VE2010000234)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(PE20120704)\|NAME=PATTEN, JAMES W.\|NAME=DANA, TODD\|(IN1897/MUMNP/2011)\|NAME=TODD DANA, COUNTRY=US \|NAME=PATTEN JAMES W, COUNTRY=US\|(AP2011005878)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(CA2752524)\|NAME=DANA, TODD, COUNTRY=US \|NAME=PATTEN, JAMES W., COUNTRY=US	(IN1897/MUMNP/2011)\|5\|(AU2010213862)\|5\|(CN102395657)\|5\|(CA2752524)\|5\|(US8323481)\|5	3	21		CARDINAL ENERGY HOLDINGS; FROM 2009-07-02; TO 2010-05-07	(EP2406353)\|WO2010/093684\|(CN102395657)\|WO2010/093684\|(MX319678)\|WO2010/093684\|(UA104616)\|WO2010/093684\|(EG26451)\|WO2010/093684\|(AU2010213862)\|WO2010/093684\|(ZA201106558)\|WO2010/093684\|(MA33117)\|WO2010/093684\|(BRPI1008447)\|WO2010/093684\|(TN2011000396)\|WO2010/093684\|(EA201171023)\|WO2010/093684\|(IN1897/MUMNP/2011)\|WO2010/093684\|(AP2011005878)\|WO2010/093684\|(IL214555)\|WO2010/093684\|(CA2752524)\|WO2010/093684		Primary examiner: Pardo Torre, J\|\|Primary examiner: Pardo Torre, J\|\|(US8323481)\|Number of Claims: NCL=12\|Number of Drawings: NDR=5\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=169\|Primary examiner: McCaig Brian\|Art Unit.: ART =1774\|\|(US20100200465)\|Number of Claims: NCL=26\|Number of Drawings: NDR=5\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1,14\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: McCaig Brian\|Art Unit.: ART =1774\|\|(WO2010/093684)\|Number of Claims: NCL=26\|Extended kind: EXTK=z\|\|(CN102395657)\|Number of Claims: NCL=26\|Gazette date: GAZDATE=2012-03-28\|Gazette number: GAZNUM=28-13\|Substantial examination effective date: 20120509\|Number of Pages: NPAGES=26\|\|(MX2011008525)\|Number of Claims: NCL=26\|Number of Pages: NPAGES=92\|\|(AU2010213862)\|Number of Claims: NCL=24\|\|(AU2010213862)\|Number of Claims: NCL=26\|\|(IN1897/MUMNP/2011)\|Number of Claims: NCL=26\|\|(AP2011005878)\|Gazette date: GAZDATE=2011-10-31\|\|(CA2752524)\|Number of Claims: NCL=26\|Number of Pages: NPAGES=46\|	(US8323481)\|Provisional Appl: US61/152,220 FDD=2009-02-12 [2009US-61152220]\|Previous publication: US20100200465 A1 2010-08-12 [US20100200465]	(EP2406353)\|ENGLISH (ENG)	(BR201008447)\|Patent\|(GE201406167)\|Patent\|(EP2406353)\|Patent\|(MY-152266)\|Patent\|(MX-319678)\|Patent\|(UA-104616)\|Patent\|(EG--26451)\|Patent\|(AU2010213862)\|Patent\|(TN2011000396)\|Patent\|(ZA201106558)\|Patent\|(US8323481)\|Patent\|(VE2010000234)\|Patent\|(PE201200704)\|Patent\|(EA201171023)\|Patent\|(CN102395657)\|Patent\|(MA--33117)\|Patent\|(IN2011MN01897)\|Patent\|(EP2406353)\|Patent\|(MX2011008525)\|Patent\|(AP2011005878)\|Patent\|(IL-214555)\|Patent\|(AU2010213862)\|Patent\|(WO201093684)\|Patent\|(CA2752524)\|Patent\|(WO201093684)\|Patent\|(US20100200465)\|Patent	Titre: (EP2406353)\|Carbon management and sequestration from encapsulated control infrastructures Résumé: (EP2406353)\|A method of sequestering carbon dioxide emissions during recovery of hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure (100). This constructed infrastructure (100) defines a substantially encapsulated volume. A comminuted hydrocarbonaceous material can be introduced into the control infrastructure (100) to form a permeable body (120) of hydrocarbonaceous material. The permeable body (120) can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure (100) is a fixed structure. Additionally, during heating, any carbon dioxide that is produced can be sequestered. Removed hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.	31	Abstract	gpt-4o-mini	no	The article focuses on carbon sequestration during hydrocarbon recovery, which does not involve accelerated weathering of minerals or the specific processes related to CO₂ capture through mineral alteration.
29	US63/469,108P\|US18/814,312\|US18/909,669\|WOUS2024/013913	US18/909,669\|WOUS2024/013913	US20250250199\|WO2024/248905	112475776	US20250250199 A1 2025-08-07 [US20250250199]\|WO2024/248905 A1 2024-12-05 [WO2024248905]	2023-05-26\|2024-02-01\|2024-08-23\|2024-10-08	2024-10-08\|2024-02-01	2025-08-07\|2024-12-05		(US20250250199)\|2044-02-01\|(WO2024/248905)\|2026-11-26	(US20250250199)\|Carbon-Sequestering Concrete Composition with Enhanced CO2 Absorbtion and Method of Manufacturing Thereof	(US20250250199)\|A carbon-sequestering concrete composition and method of production are disclosed. The composition comprises geopolymer binder components, aggregates, and alginate beads formed from brown algae powder through ionic gelation. The alginate beads significantly increase CO2 absorption surface area compared to algae powder, creating a matrix across the concrete surface that enhances long-term sequestration and improves durability. The beads interact synergistically with other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag, to enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The alginate beads also facilitate the dissolution of minerals like olivine, further enhancing carbon capture. The composition demonstrates superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. The method includes forming alginate beads, incorporating them into the concrete mixture, and allowing for initial hardening and drying processes that promote carbon dioxide absorption directly from the air.	LAFAVE MICHAEL ([US])\|LAFAVE MICHAEL ([US])	(US20250250199)\|Lafave Michael ([US])\|(WO2024/248905)\|LAFAVE, Michael ([US])	LAFAVE MICHAEL	(US20250250199)\|Lafave Michael	(WO2024/248905)\|SCHELL, Jeffrey ([US])	(US20250250199)\|The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture.\|This makes them significantly more effective for CO2 absorption compared to red and green algae species. The use of brown algae provides a more efficient and targeted approach to carbon sequestration in concrete, leveraging their natural adaptations to marine environments.\|By addressing the limitations of previous approaches, this invention represents a significant advancement in sustainable construction materials, offering superior carbon sequestration capabilities, enhanced durability, and improved overall performance.The preferred embodiment of the present invention addresses the limitations of previous approaches by utilizing brown algae species, particularly “Macrocystis pyrifera”, which have evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions.\|By incorporating these innovative features, the preferred embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|The preferred embodiment comprises a carbon-sequestering concrete and the associated methods of manufacture, addressing the limitations of previous methods and significantly enhancing CO2 absorption capabilities.\|	(US20250250199)\|1. A method of producing a carbon-sequestering concrete comprising: mixing sand and gravel aggregates while dry; adding and dry blending geopolymer binder components comprising at least one of slag, fly ash class C, fly ash class F, metakaolin, or silica fume; forming alginate beads by ionic gelation of brown algae powder; adding the alginate beads to the dry mixture of aggregates and geopolymer binder components; slowly incorporating water while mixing to achieve a workable concrete consistency; and pouring the concrete mixture into molds or forms for casting.\|6. A carbon-sequestering concrete composition comprising: 35-50% geopolymers comprising at least one of ground granulated blast furnace slag, class C fly ash, class F fly ash, metakaolin, or silica fume; 30-45% sand; 15-25% coarse aggregates comprising gravel or crushed stone; 5-10% water; and 1-5% alginate beads formed from brown algae powder.\|11. A carbon-sequestering concrete composition comprising: a geopolymer binder; aggregates; alginate beads formed from brown algae powder through ionic gelation; and at least one carbon dioxide sequestration enhancer selected from the group consisting of biochar, calcium carbonate, magnesium carbonate, magnesium silicate, olivine, and basalt rock dust.\|15. A carbon-sequestering concrete composition comprising: 30-60% aluminosilicate materials selected from the group consisting of: fly ash, ground granulated blast furnace slag, metakaolin, and silica fume; 30-50% CO2-absorbing materials selected from the group consisting of: magnesium silicate, olivine, biochar, calcium carbonate, and magnesium carbonate; 10-20% aggregates selected from the group consisting of: natural and recycled aggregates; 5-10% alkaline activators selected from the group consisting of: sodium hydroxide and sodium silicate; 5-15% algae-derived components selected from the group consisting of: silica from algae, algae biomass, and alginate beads; 1-5% carbonation accelerators; and 4-6% water; wherein the composition is capable of sequestering at least 400 kg of CO2 per 1,000 kg of concrete produced.\|	(US20250250199)\|The present invention relates to the field of sustainable construction materials, specifically to carbon-sequestering concrete compositions and methods for their production.\|The present invention seeks to overcome these limitations by providing a novel carbon-absorbing concrete composition and method of production that offers superior CO2 sequestration capabilities, enhanced durability, and improved overall performance compared to existing technologies.The present invention relates to a carbon-sequestering concrete composition and method of production that addresses the limitations of previous approaches to reducing the carbon footprint of concrete.\|	(US20250250199)\|ALGINATE BEAD(100,111)\|CARBON SEQUESTERING(100,25)\|CARBON SEQUESTERING CONCRETE(100,2)\|ENHANCED CO2 ABSORPTION(100,1)\|WORKABLE CONCRETE CONSISTENCY(72,1)\|SEQUESTRATION ENHANCER(60,1)\|SILICA FUME(57,9)\|IONIC GELATION(53,16)\|BLENDING GEOPOLYMER BINDER COMPONENT(49,1)\|CARBONATION ACCELERATOR(48,7)\|SUSTAINED CO2 ABSORPTION(47,3)\|GEOPOLYMER BINDER(46,4)\|GEOPOLYMER BINDER COMPONENT(46,2)\|CARBON DIOXIDE SEQUESTRATION ENHANCER(45,1)\|AGGREGATE(44,6)\|ALGAE BIOMASS(39,9)\|BROWN ALGAE POWDER(38,13)\|METAKAOLIN(37,11)\|BROWN ALGAE(35,28)\|ENHANCING DURABILITY(34,3)\|CO2 ABSORPTION(33,28)\|MACROCYSTIS PYRIFERA(31,11)\|NATURAL ADAPTATION(31,1)\|ALKALINE ACTIVATOR(30,3)\|RECYCLED AGGREGATE(29,6)\|SAND MIX(29,1)\|FLY ASH(28,21)\|BROWN ALGAE SPECIES(28,5)\|CO2 ABSORPTION CAPABILITY(27,2)\|LEVER AGING(27,1)\|CONCRETE(26,58)\|OLIVINE(25,23)\|SLAG(24,1)\|HARDENING(23,2)\|GEOPOLYMER COMPOUND(23,1)\|CO2 SEQUESTRATION CAPABILITY(22,11)\|CARBON SEQUESTRATION CAPABILITY(22,10)\|GREEN ALGAE SPECIES(22,2)\|BASALT(22,1)\|BIOCHAR(22,1)\|COARSE AGGREGATE(22,1)\|CRUSHED STONE(22,1)\|GEOPOLYMER(21,7)\|ALGINATE SOLUTION(20,10)\|SERVICE LIFE(20,10)\|MAGNESIUM SILICATE(20,9)\|ALGAE DERIVED COMPONENT(20,2)\|CONCRETE CARBON FOOTPRINT(20,2)\|GRAVEL(20,1)\|CARBON SEQUESTRATION(19,51)\|ACTIVATED BIOCHAR(19,2)\|SALT CONCENTRATION(19,2)\|MAGNESIUM CARBONATE(18,20)\|CASTING(18,1)\|BEAD(17,29)\|GROUND GRANULATED BLAST FURNACE SLAG(17,20)\|CALCIUM SILICATE HYDRATE(17,5)\|SEA CONDITION(17,2)\|ENHANCING CARBON CAPTURE(17,1)\|CALCIUM CARBONATE(16,22)\|CONCRETE TON(16,11)\|SYNERGISTIC INTERACTION(16,11)\|CROSSLINKING ION(16,4)\|GROUND OLIVINE(16,2)\|FLY ASH CLASS F(16,1)\|SAND(16,1)\|CONCRETE MATRIX(15,14)\|CRUCIAL ROLE(15,13)\|ALUMINOSILICATE MATERIAL(15,4)\|DUST(15,1)\|ALGAE(14,11)\|CONCRETE COMPONENT(14,9)\|SUPERPLASTICIZER(14,2)\|MARINE ENVIRONMENT(14,1)\|POROUS STRUCTURE(13,5)\|NEGATIVE NET CARBON FOOTPRINT(13,4)\|GEOPOLYMER BINDER FOUNDATION(13,2)\|CO2(12,28)\|CARBON DIOXIDE(12,24)\|CARBON DIOXIDE CAPTURE(12,10)\|NET NEGATIVE(12,4)\|POZZOLANIC REACTION ENHANCEMENT(12,4)\|CARBON FOOTPRINT(11,11)\|BASALT ROCK DUST(11,3)\|CARBON DIOXIDE ABSORPTION(11,2)\|GREEN ALGAE(11,2)\|CONCRETE SERVICE LIFE(10,6)\|MG2SIO(10,6)\|SODIUM SILICATE(10,6)\|CO2 ABSORBING MATERIAL(10,4)\|ECONOMIC VIABILITY(10,4)\|DRYING(10,2)\|MINERAL GRADUAL DISSOLUTION(10,2)\|ROBUST CELL WALL(10,2)\|SEED(10,1)\|CONCRETE MIXTURE(9,9)\|SODIUM HYDROXIDE(9,4)\|CLASS C FLY ASH(9,1)\|FLY ASH CLASS C(9,1)\|FORMED ALGINATE BEAD(9,1)\|OLIVINE GRADUAL DISSOLUTION(9,1)\|MOISTURE RETENTION(8,23)\|SELF HEALING(8,15)\|NATURAL AGGREGATE(8,6)\|ALGINATE POLYMER(8,4)\|BICARBONATE HCO3 ION(8,4)\|ADDITIVE CO2 SEQUESTRATION CAPABILITY(8,2)\|ALGINATE DROPLET(8,2)\|BEAD OPTIMIZATION(8,2)\|SPHERICAL ALGINATE BEAD FORMATION(8,2)\|ALGAE BIOMASS UPTAKE(8,1)\|CHEMICAL REACTION NATURE(8,1)\|CONCRETE PRODUCER FINANCIAL SITUATION(8,1)\|INNOVATIVE CONCRETE PRICE(8,1)\|LONG TERM SEQUESTRATION(7,8)\|SUSTAINABLE CONSTRUCTION MATERIAL(7,6)\|CONCRETE ABILITY(7,5)\|STABLE CARBONATE COMPOUND(7,5)\|CO2 DISSOLUTION(7,4)\|DROPLET SIZE(7,4)\|CONCRETE CARBON SEQUESTRATION CAPABILITY(7,3)\|AIR ENTRAIN(7,2)\|CONCRETE CURE(7,2)\|DISSOLVED CO2 INTERACTION(7,2)\|ENHANCING CO2 SEQUESTRATION(7,2)\|ADDITIVE GRADUAL DISSOLUTION(7,1)\|CLASS F FLY ASH(7,1)\|IMMENSE ENVIRONMENTAL BURDEN(7,1)\|CLASS F(6,6)\|CONCRETE FORMULATION(6,2)\|TAX BENEFIT(6,2)\|ACTIVATOR CAREFUL BALANCE(6,1)\|FINANCIAL INCENTIVE(6,1)\|TAX CREDIT ECONOMIC BENEFIT(6,1)\|CARBONIC ACID(5,9)\|CONCRETE STRUCTURE INTEGRITY(5,5)\|CARBON SEQUESTRATION POTENTIAL(5,4)\|WORKABILITY(5,4)\|ABSORB CO2(5,3)\|CO2 ABSORPTION PERIOD(5,3)\|CONCRETE CARBON CAPTURE CAPABILITY(5,3)\|CONCRETE PRODUCTION ENVIRONMENTAL IMPACT(5,3)\|CONCRETE STRENGTH(5,3)\|CLASS C(5,2)\|CONCRETE AGE(5,2)\|CONCRETE CAPABILITY(5,2)\|CONCRETE INTERNAL CURING(5,2)\|CREATING ALGINATE(5,2)\|CRITICAL INNOVATION(5,2)\|STABLE CARBONATE MINERAL(5,2)\|ALGAE CONCRETE TECHNOLOGY LIMITATION(5,1)\|ALGINATE BEAD ABILITY(5,1)\|ALGINATE BEAD UNIFORM DISTRIBUTION(5,1)\|BASALT DISSOLUTION(5,1)\|CARBON SEQUESTERING COMPETITIVENESS(5,1)\|CAREFUL DOCUMENTATION(5,1)\|CO2 CAPTURE(5,1)\|COMPOUND SEQUESTRATION(5,1)\|CONCRETE INTEGRITY(5,1)\|CONCRETE LIFESPAN(5,1)\|CONCRETE MIXER INVESTMENT(5,1)\|CONCRETE OPTION(5,1)\|CONCRETE OVERALL SEQUESTRATION CAPACITY(5,1)\|CONCRETE SUSCEPTIBILITY(5,1)\|DERIVED ALGINATE BEAD(5,1)\|ENHANCE CO2 UPTAKE(5,1)\|ENHANCE CONCRETE CO2 SEQUESTRATION CAPABILITY(5,1)\|ENHANCING CO2 ABSORPTION(5,1)\|GEOPOLYMER PRECURSOR(5,1)\|MAXIMIZE CO2 SEQUESTRATION CAPABILITY(5,1)\|MAXIMIZE ELIGIBILITY(5,1)\|METAKAOLIN INCLUSION(5,1)\|NET EARNINGS SEQUESTRATION(5,1)\|PROLONGED SEQUESTRATION(5,1)\|RELEVANT REGULATORY REQUIREMENT(5,1)\|SCIENTIFIC APPARATUS RESERVOIR(5,1)\|SEAWATER INCORPORATION(5,1)\|STABLE CALCIUM CARBONATE FORMATION(4,7)\|CONCRETE DURABILITY(4,6)\|PERIOD EXTENSION(4,6)\|ACCOUNTING(4,3)\|CURING PERIOD(4,3)\|INVESTMENT TAX CREDIT(4,3)\|IONIC GELATION(4,3)\|TONNE(4,3)\|BICARBONATE ION(4,2)\|NET CARBON SEQUESTRATION(4,2)\|STRUCTURAL REQUIREMENT(4,2)\|SUSTAINABLE CONSTRUCTION PRACTICE(4,2)\|ABSORBED CO2(4,1)\|ACCELERATION STRENGTH GAIN(4,1)\|APPLICABLE INCENTIVE(4,1)\|APPLICABLE TAX CREDIT(4,1)\|CAPTURED CO2 REMAINS(4,1)\|CARBON SEQUESTERING ADOPTION(4,1)\|CO2 ABSORPTION SITE(4,1)\|CO2 EMISSION(4,1)\|CONCRETE MIXTURE SUSTAINABILITY(4,1)\|CRACK REPAIR(4,1)\|DRIED ALGAE POWDER(4,1)\|ENHANCED ALGINATE BEAD FORMATION(4,1)\|ENHANCED CO2 SEQUESTRATION CAPABILITY(4,1)\|ENHANCING REACTIVITY(4,1)\|FUCUS SPECIES(4,1)\|INVENTOR OBSERVATION(4,1)\|MAGNESIUM ION RELEASE(4,1)\|MOIST ENVIRONMENT(4,1)\|MOISTURE ABSORPTION(4,1)\|PORE INTERCONNECTION(4,1)\|PROJECT REQUIREMENT(4,1)\|RAPID CARBONATION REACTION(4,1)\|SEQUESTERING CARBON(4,1)\|SILICA DISSOLUTION(4,1)\|SILICA FUME FINE PARTICLE(4,1)\|TON BATCH(4,1)\|TRACE MINERAL(4,1)\|LOCALIZED HIGH HUMIDITY ENVIRONMENT(3,17)\|CALCIUM HYDROXIDE(3,4)\|DROPWISE(3,4)\|NAOH(3,4)\|CALCIUM ALUMINATE HYDRATE(3,2)\|CAPTURING CARBON DIOXIDE(3,2)\|CEMENT HYDRATION(3,2)\|CONCRETE MIXTURE REQUIREMENT(3,2)\|DIVALENT CATION(3,2)\|EARLY STRENGTH(3,2)\|EXCESS ION(3,2)\|MAGNESIUM CARBONATE FORMATION(3,2)\|STATE TAX INCENTIVE(3,2)\|ACTIVE CO2 ABSORPTION(3,1)\|ADDRESS ENVIRONMENTAL CONCERN(3,1)\|ADJUSTED PARAMETER(3,1)\|ALGINATE CONTENT(3,1)\|APPLICABLE REGULATION(3,1)\|CALCIUM CARBONATE PRECIPITATE(3,1)\|CARBON CAPTURE OPPORTUNITY(3,1)\|CARBON CAPTURING CONCRETE(3,1)\|CARBON DIOXIDE GIGATON(3,1)\|CO2 ABSORPTION INCONSISTENT LEVEL(3,1)\|CO2 SEQUESTRATION POTENTIAL(3,1)\|CO2 UPTAKE RATE(3,1)\|COMBINED TAX CREDIT(3,1)\|CONCRETE CARBON CAPTURE CAPACITY(3,1)\|CONCRETE CO2 ABSORPTION CAPACITY(3,1)\|CONTRIBUTOR(3,1)\|DEPICTION(3,1)\|DISCRETE PARTICLE(3,1)\|EMISSION SCALE(3,1)\|EXPERIMENTATION(3,1)\|EXTENDED ABSORPTION WINDOW(3,1)\|FEAT(3,1)\|INCREASED MINERAL CARBONATION POTENTIAL(3,1)\|INNOVATIVE ALGAE DERIVED COMPONENT(3,1)\|MAXIMIZE CO2 ABSORPTION CAPACITY(3,1)\|MICROCRACK(3,1)\|MIXED ALGAE(3,1)\|MIXING ALGAE(3,1)\|MOISTURE RETENTION ENHANCEMENT(3,1)\|RELEASED MAGNESIUM ION(3,1)\|SOLID ALGAE POWDER PARTICLE(3,1)\|STABLE MINERAL(3,1)\|STARK CONTRAST(3,1)\|SUSTAINABLE SILICA SOURCE(3,1)\|CONSTRUCTION MATERIAL(2,7)\|GEOPOLYMERIZATION(2,3)\|INCREASED MOISTURE CONTENT(2,3)\|KEY COMPONENT(2,2)\|\|(WO2024/248905)\|CARBON DIOXIDE(100,42)\|GEOPOLYMER CONCRETE(100,21)\|CARBON SEQUESTERING(100,10)\|SIDEWALK(100,10)\|ATMOSPHERIC CARBON DIOXIDE(100,8)\|BINDER(100,8)\|DRIED MARINE ALGA POWDER(100,7)\|CARBON SEQUESTERING GEOPOLYMER CONCRETE(100,4)\|CARBON SEQUESTERING CONCRETE(100,2)\|SIDEWALK CARBON SEQUESTERING(100,1)\|DRIED MARINE ALGA(94,9)\|GEOPOLYMERIC BINDER PRECURSOR(83,1)\|ALKALINE ACTIVATOR(70,4)\|FINISHED PEDESTRIAN INFRASTRUCTURE(69,1)\|SILICA FUME(67,10)\|WORKABLE CONCRETE CONSISTENCY(64,2)\|INNATE CO2 AFFINITY(61,1)\|FREEZE THAW RESILIENCE(60,4)\|GEOPOLYMER ALGAE CONCRETE SLAB(59,1)\|SERVICE LIFETIME(58,4)\|INTERGROUND LIMESTONE INCORPORATION(57,1)\|COARSE AGGREGATE(56,14)\|BLENDING GEOPOLYMER BINDER COMPONENT(56,1)\|METAKAOLIN(51,6)\|GEOPOLYMER ALGAE CONCRETE MIXTURE(51,2)\|SIDEWALK SEGMENT(51,1)\|ENHANCED FREEZE THAW RESILIENCE(49,1)\|FINE AGGREGATE(48,6)\|GEOPOLYMER BINDER(46,7)\|MARINE MACROALGAE(46,3)\|FRESHWATER SPECIES(44,1)\|CARBON MINERALIZATION REACTION(42,1)\|ENHANCED CARBON MINERALIZATION(41,4)\|CONCRETE SLAB MATRIX(41,1)\|CRITICAL URBAN GROWTH(41,1)\|RENEWAL EFFORT(41,1)\|SIDEWALK ADOPTION(41,1)\|RE USE(40,1)\|SIDEWALK SEGMENT SHAPE(39,1)\|SAND MIX(37,2)\|GEOPOLYMER(36,24)\|GEOPOLYMER PRECURSOR(36,7)\|LOGISTICAL BARRIER(36,2)\|FUCUS SPECIES(35,3)\|ALGAE ADDITIVE(35,2)\|LIMESTONE POWDER(35,2)\|PERIODIC WETTING(35,2)\|GEOPOLYMERIC BINDER PHASE(34,2)\|ALKALI ACTIVATOR(33,3)\|ALGAE POWDER(32,17)\|FLY ASH(31,17)\|ANGULAR CRUSHED PARTICLE(31,1)\|INTEGRATED ALGAE POWDER(31,1)\|CONCRETE(30,46)\|GEOPOLYMER BINDER COMPONENT(30,4)\|ATMOSPHERIC CARBON DIOXIDE MINERALIZATION(30,1)\|ALGINATE POLYMER(29,4)\|THICKNESS CONCRETE SLAB(29,1)\|AGGREGATE(28,10)\|GROUND GRANULATED BLAST FURNACE SLAG(27,10)\|ALKALI ACTIVATOR SOLUTION(27,4)\|DRIED ALGAE(27,3)\|DRIED SALT(27,1)\|LB CARBON DIOXIDE(27,1)\|CONCRETE MIXTURE(26,9)\|CEMENTITIOUS MATERIAL(26,8)\|ECO FRIENDLY CONSTRUCTION(26,1)\|EXTENDED DURABILITY(26,1)\|STABLE CALCIUM CARBONATE(26,1)\|CARBON DIOXIDE EMISSION(25,4)\|DOLOMITIC SAND(25,3)\|INTEGRATED DRIED MARINE ALGA(25,1)\|GEOPOLYMER MATRIX(24,5)\|MARINE ALGA(24,5)\|LAMINARIA(24,3)\|DURATION EXTENSION(24,2)\|ALGAE DERIVED CALCIUM ION(24,1)\|CONCRETE SLAB(24,1)\|SEA SALT(23,16)\|CO2 ABSORPTION(23,13)\|CO2 ABSORBING CONCRETE(23,3)\|MAGNESIUM ION(22,6)\|CALCIUM OXIDE POWDER(22,3)\|DRYING CYCLE(22,2)\|GEOPOLYMER COMPOUND(22,2)\|ASCOPHYLLUM(21,3)\|TRANSPORTATION COST(21,3)\|COARSE AGGREGATE INTRODUCTION(21,2)\|GREENHOUSE EMISSION(21,1)\|REACTIVE AGGREGATE MATERIAL(21,1)\|CUBIC YARD(20,4)\|DRY MIXER BLEND(20,4)\|MAGNESIUM OXIDE POWDER(20,4)\|SARGASSUM(20,3)\|SLAB(20,2)\|COMPOSITION CURE(20,1)\|CUMULATIVE REMOVAL(20,1)\|BINDER MATRIX(18,9)\|ENHANCING DURABILITY(18,2)\|WORKABILITY TARGETED LEVEL(18,2)\|FLY ASH CLASS F(18,1)\|MEASURED INCREMENT(18,1)\|CRUSHED STONE(17,4)\|ADOPTION(17,2)\|FINISHING EQUIPMENT(17,2)\|INLAND CONSTRUCTION SITE(17,2)\|PACKING DENSITY CONSOLIDATION(17,2)\|CARBON DIOXIDE TON(17,1)\|CARBON NEGATIVE PERFORMANCE CREDENTIALS(17,1)\|WINTER CONDITION(17,1)\|SEAWATER(16,17)\|SODIUM SILICATE(16,4)\|LIFETIME(16,3)\|CARBON DIOXIDE LB(16,1)\|LARGE CONSUMER(16,1)\|STANDARD CONCRETE MIX(16,1)\|SLAG(15,8)\|SODIUM HYDROXIDE(15,4)\|CASTING(15,3)\|FINAL CONCRETE(15,3)\|SEAWATER LARGE VOLUME(15,1)\|URBAN PEDESTRIAN INFRASTRUCTURE RENEWAL(15,1)\|SAND(14,12)\|CALCIUM OXIDE REACTIVITY(14,2)\|SEMIANGULAR SHAPE(14,2)\|REACTIVE MAGNESIUM OXIDE(14,1)\|CO2(13,32)\|GRAVEL(13,6)\|ALUMINOSILICATE SOURCE MATERIAL(13,2)\|PREVENT LOCALIZED SETTING(13,1)\|CALCIUM OXIDE(12,13)\|MAGNESIUM OXIDE(12,11)\|MAGNESIUM CARBONATE(12,4)\|INTERRUPTION(12,3)\|BROWN ALGAE GROUP(12,2)\|CALCIUM ION(12,2)\|CALCIUM CARBONATE(11,6)\|DRIED MARINE SALT(11,6)\|CONCRETE MIXER(11,2)\|TARGET LEVEL(11,2)\|BURNING ANTHRACITE BYPRODUCT(11,1)\|BYPRODUCT GEOPOLYMER INCORPORATION(11,1)\|EQUIPMENT LIFETIME(11,1)\|GEOPOLYMERIC ALUMINOSILICATE PRECURSOR(11,1)\|INTRINSIC MINERAL CARBONATION REACTIVITY(11,1)\|METAKAOLIN GEOPOLYMER BINDER(11,1)\|MITIGATE SUSTAINABILITY ISSUE(11,1)\|OCEAN ECOSYSTEM DEPLETION(11,1)\|CONCRETE MATRIX(10,5)\|GEOPOLYMERIZATION REACTION(10,5)\|MGO AVAILABILITY(10,3)\|ALUMINOSILICATE MATERIAL(10,2)\|SIDEWALK SLAB(10,2)\|METAKAOLIN GEOPOLYMERIC BINDER(10,1)\|CLASS C FLY ASH(9,7)\|DURABLE INFRASTRUCTURE(9,2)\|GEOPOLYMERIC PRECURSOR(9,2)\|LOGISTICAL CHALLENGE(9,2)\|PRODUCTIVE REUSE(9,2)\|AGGREGATE SUITABLENESS EVALUATION(9,1)\|ALGAL BIOMASS ASH(9,1)\|ALGAL COMPOUND BIORECEPTIVITY(9,1)\|CARBON DIOXIDE ABSORPTION CAPACITY(9,1)\|CONCRETE OVER CUBIC YARD(9,1)\|GLOBAL EMISSION INFRASTRUCTURE SHARE(9,1)\|HYBRID GEOPOLYMER ALGAE CONCRETE(9,1)\|MARINE SEAWATER ALGAE(9,1)\|PEDESTRIAN INFRASTRUCTURE PROJECT(9,1)\|REPURPOSING INDUSTRIAL BYPRODUCT(9,1)\|URBAN ROAD INFRASTRUCTURE(9,1)\|CARBON ABSORBING GEOPOLYMER CONCRETE(8,5)\|DRIED ALGAE POWDER(8,3)\|MINERAL REACTION(8,3)\|PARTICLE SIZE(8,3)\|CEMENT COMPONENT(8,2)\|CHEMICAL REACTION NATURE(8,2)\|CONCRETE WORKABILITY(8,2)\|EMISSION POUND(8,2)\|FLY ASH CLASS C(8,2)\|MAJOR COMPATIBILITY ISSUE(8,2)\|BYPRODUCT TON(8,1)\|GEOPOLYMER ALGAE CONCRETE CURE(8,1)\|GEOPOLYMER ALGAE CONCRETE FORMULATION(8,1)\|GEOPOLYMER CONSTITUENT CARBONATE(8,1)\|GEOPOLYMERIZATION POLYMER CROSSLINKING(8,1)\|IMMENSE ENVIRONMENTAL BURDEN(8,1)\|OPTIMIZED GEOPOLYMER ALGAE CONCRETE(8,1)\|ROAD CO2 FOOTPRINT(8,1)\|SLOW SEAWATER DIFFUSION KINETICS(8,1)\|SUSTAINABLE AQUACULTURE(8,1)\|VISUAL MICROSTRUCTURAL VERIFICATION(8,1)\|CLASS F FLY ASH(7,5)\|ALGAL COMPONENT(7,4)\|CARBONATION POTENTIAL(7,2)\|CONCRETE USAGE(7,2)\|FAST GROWING(7,2)\|AGGREGATE HOMOGENEOUS DISPERSION(7,1)\|ALGAE CO2 ABSORPTION(7,1)\|ALGAL BIOMASS MINERAL COMPOSITE(7,1)\|BYPRODUCT SLAG(7,1)\|CARBON MINERALIZE ALGAL BIOMASS(7,1)\|CARBONATION KINETICS(7,1)\|DRIED ALGAE REHYDRATE(7,1)\|INVENTOR ALGAE ADDITIVE(7,1)\|LIFECYCLE THREAT(7,1)\|MEETING STRINGENT PURITY(7,1)\|MILE INLAND(7,1)\|MINERAL CARBONATION SITE(7,1)\|PERSISTENT CARBON MINERALIZATION(7,1)\|SEAWATER HUNDRED ENORMOUS VOLUME(7,1)\|SELECTIVE PRESSURE(7,1)\|SLAG BALANCED BLEND(7,1)\|TRANSPORTABLE MARINE SALT(7,1)\|UNIFORMLY GRADED AGGREGATE(7,1)\|WIDESCALE ADOPTION(7,1)\|WIDESPREAD COMMERCIAL ADOPTION(7,1)\|CURING(6,4)\|EARLY STRENGTH(6,3)\|LARGE VOLUME(6,3)\|ALGAE BEARING GEOPOLYMER CONCRETE(6,2)\|CARBONATE PRECIPITATION(6,2)\|CARBONATION REACTION(6,2)\|CELL WALL(6,2)\|CLASS F(6,2)\|CO2 UPTAKE CAPACITY(6,2)\|CURING CONCRETE(6,2)\|DRYING(6,2)\|MECHANICAL STRENGTH(6,2)\|MINERAL CARBONATE FORMATION(6,2)\|WATER BINDER RATIO(6,2)\|ACTIVELY ABSORB AMBIENT CO2(6,1)\|ACTIVELY ABSORBING CO2(6,1)\|ALGAE BIOMASS ASH(6,1)\|ALGAL ASH(6,1)\|ALGAL BIOMASS CONTENT(6,1)\|CANDIDATE SAND TESTING(6,1)\|CARBON DIOXIDE OVER(6,1)\|CARBON MINERALIZATION FUNCTIONALITY(6,1)\|CARBONATE DIFFRACTION PEAK INTENSITY(6,1)\|CARBONATION CURING(6,1)\|CO2 EMISSION TON(6,1)\|CO2 EMISSION YEAR(6,1)\|CO2 ENHANCING DIFFUSION(6,1)\|CONTINUAL CULTIVATION(6,1)\|CRUSHED SAND PARTICLE(6,1)\|DOLOMITIC AGGREGATE(6,1)\|DYNAMICS COMPETITION(6,1)\|ECONOMIC BINDER OPTION(6,1)\|ENHANCED CO2 MINERALIZATION CAPACITY(6,1)\|ENHANCING MATRIX COHESION(6,1)\|ERECTED ONSITE(6,1)\|FELDSPATHIC SAND(6,1)\|FRESHWATER ALGA SPECIES(6,1)\|GEOPOLYMER CONCRETE LEVERAGE(6,1)\|HARDENED GEOPOLYMER CONCRETE(6,1)\|INNATE REACTIVITY(6,1)\|INTEGRATING SEAWATER(6,1)\|LIMESTONE DERIVED CAO(6,1)\|LOGISTICS BARRIER(6,1)\|LOGISTICS CONSTRAINT(6,1)\|MASSIVE SCALABILITY(6,1)\|MAXIMIZED CARBON MINERALIZATION(6,1)\|MEANINGFUL CO2 SEQUESTRATION(6,1)\|MGO PRECURSOR SITE(6,1)\|MINERAL CARBONATION CAPACITY(6,1)\|MULTIYARD BUCKET(6,1)\|PETROGRAPHIC EXAMINATION(6,1)\|PLENTIFUL CAO(6,1)\|REALISTIC VARIABILITY(6,1)\|RECYCLING PATHWAY(6,1)\|ROBUST CROSSLINKED MATRIX(6,1)\|SALINITY OCEAN ENVIRONMENT(6,1)\|SAND MINERALOGY(6,1)\|SIDEWALK LIFETIME(6,1)\|SIDEWALK SQUARE FOOT(6,1)\|SUBBITUMINOUS COAL BURNING(6,1)\|TRANSPORTATION IMPEDIMENT(6,1)\|WIDESPREAD ADOPTION(6,1)\|BINDER PHASE(5,3)\|CARBON DIOXIDE UPTAKE(5,3)\|PRIMARY BINDER(5,3)\|UNIFORM DISTRIBUTION(5,3)\|ALGAE CONTENT(5,2)\|CA DISSOLUTION(5,2)\|CO2 CAPTURE(5,2)\|CONCRETE CARBON FOOTPRINT(5,2)\|CONCRETE MANUFACTURER(5,2)\|CONCRETE PERFORMANCE(5,2)\|CONSTRUCTION SCHEDULE(5,2)\|EMISSION SCALE(5,2)\|FINAL DRY INGREDIENT(5,2)\|SUSTAINABLE INFRASTRUCTURE(5,2)\|ABUNDANT CAO(5,1)\|AGGREGATE PROPORTION(5,1)\|ALGAE BLEND(5,1)\|ALGAE SPECIES(5,1)\|ALGAL ADDITIVE(5,1)\|BINDER CONSOLIDATION(5,1)\|BLENDED GEOPOLYMER BINDER COMPONENT(5,1)\|BUILDING CONCRETE REQUIREMENT(5,1)\|CARBONATE SAND(5,1)\|CIVIC CONSTRUCTION INITIATIVE(5,1)\|CO2 POUND(5,1)\|CO2 PRECIPITATION(5,1)\|COARSE AGGREGATE PURITY(5,1)\|COMPATIBILITY CHALLENGE(5,1)\|COMPOSITIONAL MODIFICATION(5,1)\|COMPREHENSIVE EVALUATION(5,1)\|CONCRETE COMPONENT(5,1)\|CONCRETE CONSISTENCY(5,1)\|CONCRETE DRY INGREDIENT(5,1)\|CONCRETE DURABILITY(5,1)\|CONCRETE POUND(5,1)\|DISSOLVED CALCIUM ABUNDANCE(5,1)\|DRY CONCRETE CONSTITUENT(5,1)\|DURABLE SANDSTONE(5,1)\|EMISSION MITIGATION(5,1)\|EMISSION QUARTER(5,1)\|ENORMOUS EMISSION(5,1)\|EXTERIOR HARDSCAPE(5,1)\|FERROSILICON ALLOY(5,1)\|FINE LIMESTONE POWDER(5,1)\|GEOPOLYMER ALGAE CONCRETE MIX(5,1)\|GEOPOLYMERIC GEL(5,1)\|GROWING MARINE ALGA(5,1)\|HEAVY AGGREGATE(5,1)\|HIGHWAY INTEGRITY(5,1)\|HIGHWAY PROFILE(5,1)\|HIGHWAY STRETCHING(5,1)\|HOMOGENIZE FULL COMPLEMENT(5,1)\|IMPACTFUL ROUTE(5,1)\|INCORPORATED ALGAL BIOMASS(5,1)\|INFRASTRUCTURE EXPANSION(5,1)\|LIBERATED CO2(5,1)\|MAJOR CONCRETE INGREDIENT(5,1)\|MAJOR UNRESOLVED BARRIER(5,1)\|MAXIMIZE CARBON MINERALIZATION POTENTIAL(5,1)\|MEASURABLE PROGRESS(5,1)\|MICROALGAL POWDER(5,1)\|MINERAL SUITABILITY(5,1)\|NATURAL POZZOLAN(5,1)\|NET CO2 EMISSION(5,1)\|NET CO2 IMPACT(5,1)\|OFFSET MINOR IMPURITY(5,1)\|OPTIMIZED AGGREGATE SELECTION(5,1)\|OPTIMIZED REACTIVITY(5,1)\|REACTIVE BINDER IDEAL(5,1)\|SCALABLE PATHWAY(5,1)\|SCARCE LANDFILL VOLUME(5,1)\|SEAWATER CARBON ABSORPTION(5,1)\|SLAG BINDER(5,1)\|SLAG PRECURSOR(5,1)\|STRUCTURAL INFRASTRUCTURE(5,1)\|SUN DRYING(5,1)\|THERMOGRAVIMETRIC ANALYSIS(5,1)\|VARIANCE LOCALIZATION(5,1)\|WASH GRADING(5,1)\|CLASS C(4,10)\|CACO3(4,5)\|CONCRETE STRENGTH(4,5)\|MGCO3(4,5)\|ALGINATE POLYMER CHAIN(4,2)\|ALKALI SOLUTION(4,2)\|CARBON ABSORBING CONCRETE(4,2)\|CARBON DIOXIDE POUND(4,2)\|COMPONENT REACTION(4,2)\|DEFICIT(4,2)\|DEMOLDING(4,2)\|ENOUGH CALCIUM(4,2)\|FINE POWDER(4,2)\|HEAT GENERATION(4,2)\|INCOMPATIBILITY(4,2)\|PORTLAND CEMENT(4,2)\|SEA CONDITION(4,2)\|STANDARD CONCRETE MANUFACTURE(4,2)\|TRANSPORTATION INFRASTRUCTURE(4,2)\|WALKWAY(4,2)\|ABSORBED CO2(4,1)\|ABSORPTION KINETICS(4,1)\|ABUNDANT CALCIUM(4,1)\|ABUNDANT CO2(4,1)\|ABUNDANT GLOBAL SUPPLY(4,1)\|ABUNDANT ION(4,1)\|ACTIVATOR PARAMETER(4,1)\|AGGREGATE PARTICLE(4,1)\|AIRBORNE CO2(4,1)\|ALGAE DISPERSION(4,1)\|ALGAE POWDER PRODUCTION(4,1)\|ALKALI ACTIVATED ALUMINOSILICATE CHEMISTRY(4,1)\|BINDER COMPONENT INITIATE DISSOLUTION(4,1)\|BINDER INGREDIENT(4,1)\|BINDER PASTE(4,1)\|BLEND BALANCE(4,1)\|BROAD ADOPTION(4,1)\|CARBON MINERALIZATION CAPACITY(4,1)\|CHUTE DISCHARGE(4,1)\|CO2 NATURAL DIFFUSION(4,1)\|CO2 TON(4,1)\|COAL COMBUSTION(4,1)\|CONCRETE CURING(4,1)\|CONCRETE POWDER SAMPLE(4,1)\|CONCRETE SERVICE LIFE(4,1)\|CUMULATIVE CO2 REMOVAL(4,1)\|DEVELOPING CARBONATE(4,1)\|DRY AGGREGATING MIXING(4,1)\|DRYING SHRINKAGE(4,1)\|ENHANCED DIFFUSION(4,1)\|ENHANCED LONGEVITY(4,1)\|EVENLY DISTRIBUTED CAO CONTENT(4,1)\|EXTENDED SERVICE LIFETIME(4,1)\|FAST KINETICS(4,1)\|FULL BINDER BLEND CONTEXT(4,1)\|FULL CO2 MINERALIZATION CAPACITY(4,1)\|GEOPOLYMER PERFORMANCE(4,1)\|GEOPOLYMER RATIO(4,1)\|GEOPOLYMERIC COMPONENT(4,1)\|GEOPOLYMERIC COMPOUND(4,1)\|GRADE COMPACTION(4,1)\|GRADING ZONE(4,1)\|GRAVEL PARTICLE(4,1)\|GRAVIMETRIC TESTING(4,1)\|GREENHOUSE GAS RERELEASE(4,1)\|HARDENING DURATION(4,1)\|INTEGRATED MARINE SALT(4,1)\|LANDFILL LOADING(4,1)\|LANDFILL WASTE VOLUME(4,1)\|LIFECYCLE PERFORMANCE(4,1)\|MAJOR CONTRIBUTOR(4,1)\|MAJOR ECONOMIC LIMITATION(4,1)\|MAKE GEOPOLYMER CONCRETE(4,1)\|MARINE ALGA INTEGRATION(4,1)\|MASSIVE CONCRETE VOLUME(4,1)\|MASSIVE DEMAND(4,1)\|MAXIMIZE SERVICE LIFE(4,1)\|MGO REACTION(4,1)\|MIXING AGGREGATE(4,1)\|NATURAL MINERALIZATION(4,1)\|NEGATION CAPABILITY(4,1)\|OPTIMUM CONSISTENCY(4,1)\|PARTICLE DURABILITY(4,1)\|PERSISTENT CARBON SEQUESTRATION(4,1)\|PLURAL INCLUSION(4,1)\|POLYCONDENSATION REACTION(4,1)\|PORTABLE MIXER(4,1)\|POZZOLANIC QUALITY(4,1)\|PRECIPITATED CARBONATE COMPOUND(4,1)\|PRECIPITATED CARBONATE FORMATION(4,1)\|PROCESSED MARINE SALT(4,1)\|REACTIVE CAO(4,1)\|REACTIVE MINERAL ION(4,1)\|REBAR SPACING(4,1)\|RELIABLE CO2 SEQUESTRATION(4,1)\|REQUIRING REINFORCEMENT(4,1)\|ROBUST CO2(4,1)\|ROUNDED GRAIN(4,1)\|ROUNDED PARTICLE(4,1)\|SAND PROPORTION(4,1)\|SEAWATER SALT(4,1)\|SPECIALIZED CONTAINER(4,1)\|STAGNANT MICROSCOPIC WATER(4,1)\|SUPPORTING SUSTAINABILITY(4,1)\|THROUGHOUT INTACT CONCRETE SAMPLE(4,1)\|TRANSPORTATION DEPARTMENT PROJECT(4,1)\|WORKABLE MATRIX FORMATION(4,1)\|ABLE INLAND DISTRIBUTION(3,1)\|ALGAE DERIVED CALCIUM(3,1)\|ALKALI ACTIVATED SLAG(3,1)\|ALKALI ACTIVATION REACTION(3,1)\|ALKALINE ACTIVATOR SOLUTION(3,1)\|ANGULAR PARTICLE(3,1)\|ASTM CL(3,1)\|BINDER ADJUSTMENT(3,1)\|BINDER ALONE ACCOUNT(3,1)\|BINDER MANUFACTURING(3,1)\|BINDER REACTION(3,1)\|BLENDING QUALITY(3,1)\|BONDING ENHANCEMENT(3,1)\|CA REACTION(3,1)\|CALCIUM CARBONATE STABILIZATION(3,1)\|CALCIUM ION ABUNDANCE(3,1)\|CAPTURING CARBON(3,1)\|CARBAMATE FORMATION(3,1)\|CARBON DIOXIDE GIGATON(3,1)\|CARBON ENHANCED CURING REGIME(3,1)\|CARBONATE LOCK(3,1)\|CO2 ABSORPTION INCONSISTENT LEVEL(3,1)\|CO2 ABSORPTION MEANINGFUL LEVEL(3,1)\|CO2 CURING(3,1)\|CO2 LB CONCRETE(3,1)\|CO2 UPTAKE RATE(3,1)\|COASTAL ACCESS(3,1)\|CONTINUING CARBON SEQUESTRATION(3,1)\|CONTROLLED ADDITION(3,1)\|DEPICTION(3,1)\|DIVALENT CALCIUM ION(3,1)\|DRY COMPONENT(3,1)\|DRY INCORPORATION(3,1)\|DURABLE MATRIX(3,1)\|ECO FRIENDLY PRODUCTION(3,1)\|EMBODIED CARBON ABSORPTION(3,1)\|FINITE NATURAL RESOURCE(3,1)\|FLATWORK(3,1)\|FRACTURE FACE(3,1)\|GEOPOLYMER PRODUCTION(3,1)\|GLOBAL EMISSIONS REDUCTION TARGET(3,1)\|HARDENED STRENGTH(3,1)\|HARDENING REACTION(3,1)\|HEAT BUILDUP(3,1)\|HOMOGENEOUS MIXING(3,1)\|HYDROXIDE ION(3,1)\|IMMENSE CARBON REDUCTION OPPORTUNITY(3,1)\|INCONSISTENT PERFORMANCE(3,1)\|INSTALLATION CARBON ABSORPTION(3,1)\|INTERDEPENDENT CHEMICAL INTERACTION(3,1)\|KEYING(3,1)\|LIMIT FEASIBILITY(3,1)\|MANUFACTURED SAND(3,1)\|MAP CARBONATE(3,1)\|MASS ALGAE(3,1)\|MINERAL DELIVERY(3,1)\|MIXER RUN(3,1)\|NATURAL SAND(3,1)\|NEUTRAL PH(3,1)\|OPERATIONAL LIMITATION(3,1)\|ORGANIC IMPURITY(3,1)\|ORGANIC MINIMIZATION(3,1)\|PERFORMING CURING(3,1)\|PORE NETWORK(3,1)\|PRIMARY CONCRETE(3,1)\|PRODUCTION POUND(3,1)\|QUALITY GRAVEL(3,1)\|RAPID ADOPTION(3,1)\|REACTION CAPABILITY(3,1)\|READY MIX CONCRETE PRODUCTION(3,1)\|RELEASING CALCIUM(3,1)\|RELIABLE CARBON ABSORPTION(3,1)\|RENEWABLE SUPPLY(3,1)\|SALT CONCENTRATION(3,1)\|SEAWATER SOLUTION(3,1)\|SIDEWALK CONSTRUCTION ENVIRONMENTAL IMPACT(3,1)\|SIEVING(3,1)\|SILICA SAND(3,1)\|STABLE CARBONATE COMPOUND(3,1)\|STRENGTH BUILDUP(3,1)\|SUSTAINABLE HARVEST(3,1)\|TOTAL BINDER BLEND(3,1)\|TRANSFORMATIVE(3,1)\|UNIFORM AGGREGATE DISTRIBUTION(3,1)\|UNIFORM BLEND(3,1)\|URBAN SCALE(3,1)\|	(US20250250199)\|I claim:\|1. A method of producing a carbon-sequestering concrete comprising:\| mixing sand and gravel aggregates while dry;\| adding and dry blending geopolymer binder components comprising at least one of slag, fly ash class C, fly ash class F, metakaolin, or silica fume;\| forming alginate beads by ionic gelation of brown algae powder;\| adding the alginate beads to the dry mixture of aggregates and geopolymer binder components;\| slowly incorporating water while mixing to achieve a workable concrete consistency; and\| pouring the concrete mixture into molds or forms for casting.\|2. The method of claim 1, wherein forming the alginate beads comprises:\| mixing brown algae powder with water to create an alginate solution;\| introducing the alginate solution dropwise into a bath containing calcium ions; and\| collecting the formed alginate beads.\|3. The method of claim 2, wherein the brown algae powder is derived from Macrocystis pyrifera. \|4. The method of claim 1, further comprising controlling the size and density of the alginate beads by adjusting at least one of: concentration of the alginate solution, type and concentration of crosslinking ions, and droplet size.\|5. The method of claim 1, further comprising allowing an initial hardening and drying process during which the alginate beads absorb carbon dioxide directly from the air through natural chemical reactions with the geopolymer compounds.\|6. A carbon-sequestering concrete composition comprising:\| 35-50% geopolymers comprising at least one of ground granulated blast furnace slag, class C fly ash, class F fly ash, metakaolin, or silica fume;\| 30-45% sand;\| 15-25% coarse aggregates comprising gravel or crushed stone;\| 5-10% water; and\| 1-5% alginate beads formed from brown algae powder.\|7. The composition of claim 6, wherein the alginate beads are formed through ionic gelation of brown algae powder derived from Macrocystis pyrifera. \|8. The composition of claim 6, further comprising at least one of magnesium carbonate and olivine (Mg2SiO4).\|9. The composition of claim 6, wherein the alginate beads create a matrix across the surface of the concrete, increasing carbon dioxide absorption surface area compared to algae powder.\|10. The composition of claim 6, wherein the alginate beads contribute to self-healing of micro-cracks in the concrete by facilitating ongoing formation of carbonate compounds.\|11. A carbon-sequestering concrete composition comprising:\| a geopolymer binder;\| aggregates;\| alginate beads formed from brown algae powder through ionic gelation; and\| at least one carbon dioxide sequestration enhancer selected from the group consisting of biochar, calcium carbonate, magnesium carbonate, magnesium silicate, olivine, and basalt rock dust.\|12. The carbon-sequestering concrete composition of claim 11, wherein the geopolymer binder comprises at least one of fly ash, ground granulated blast furnace slag, metakaolin, or silica fume.\|13. The carbon-sequestering concrete composition of claim 11, wherein the alginate beads are formed from brown algae species Macrocystis pyrifera. \|14. The carbon-sequestering concrete composition of claim 11, further comprising carbonation accelerators in the form of calcium silicate hydrate (C—S—H) seeds.\|15. A carbon-sequestering concrete composition comprising:\| 30-60% aluminosilicate materials selected from the group consisting of: fly ash, ground granulated blast furnace slag, metakaolin, and silica fume;\| 30-50% CO2-absorbing materials selected from the group consisting of: magnesium silicate, olivine, biochar, calcium carbonate, and magnesium carbonate;\| 10-20% aggregates selected from the group consisting of: natural and recycled aggregates;\| 5-10% alkaline activators selected from the group consisting of: sodium hydroxide and sodium silicate;\| 5-15% algae-derived components selected from the group consisting of: silica from algae, algae biomass, and alginate beads;\| 1-5% carbonation accelerators; and\| 4-6% water;\| wherein the composition is capable of sequestering at least 400 kg of CO2 per 1,000 kg of concrete produced.\|16. The carbon-sequestering concrete composition of claim 15, wherein the aluminosilicate materials comprise 30% fly ash (Class F), 20% ground granulated blast furnace slag, 5% metakaolin, and 3% silica fume.\|17. The carbon-sequestering concrete composition of claim 15, wherein the CO2-absorbing materials comprise 15% magnesium silicate, 15% finely ground olivine, 10% activated biochar, 3% calcium carbonate, and 2% magnesium carbonate.\|18. The carbon-sequestering concrete composition of claim 15, wherein the algae-derived components comprise 1% silica from algae, 3% algae biomass for bead formation, and 5% alginate beads.\|19. The carbon-sequestering concrete composition of claim 15, further comprising 0.5% superplasticizers and 0.1% air-entraining agents.\|20. The carbon-sequestering concrete composition of claim 15, wherein the composition has a net negative carbon footprint of at least 300 kg CO2 per 1,000 kg of concrete produced.	(US20250250199)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] This application claims the benefit of and incorporates by reference in its entirety U.S. Provisional Patent Application No. 63/469,108, filed May 26, 2023 which is incorporated herein by reference in its entirety. This application also claims the benefit of, is a continuation-in-part of, and incorporates by reference in its entirety U.S. patent application Ser. No. 18/722,678, filed on Jun. 21, 2024, and U.S. patent application Ser. No. 18/814,312 filed on Aug. 23, 2024. This application also claims the benefit of and incorporates by reference in its entirety International Patent Application No. PCT/US24/13913, filed Feb. 1, 2024.\|(US20250250199)\|FIELD OF THE INVENTION\|[0002] The present invention relates to the field of sustainable construction materials, specifically to carbon-sequestering concrete compositions and methods for their production.\|BACKGROUND OF THE INVENTION\|[0003] Concrete is one of the most widely used construction materials globally, with over 4 billion metric tons produced annually.\|[0004] However, conventional Portland cement concrete production is a significant contributor to global carbon dioxide emissions, accounting for 7-8% of all CO2 emissions worldwide. This represents an immense environmental burden, generating over 2 gigatons of carbon dioxide per year during cement production alone.\|[0005] Recent efforts to mitigate the carbon footprint of concrete have explored various approaches, including the incorporation of seawater and algae into concrete mixes to enable CO2 sequestration.\|[0006] However, these existing methods have achieved only modest and inconsistent levels of CO2 absorption that pale in comparison to the scale of emissions from concrete production.\|[0007] One such approach is described in Korean Patent No. 102079643 B1 to Lee et al. (“LEE”), which discloses a carbon dioxide-absorbing marine concrete composition made by mixing blast furnace slag, fly ash, metakaolin, sodium silicate, and dried algae powder. While this composition attempts to address the environmental impact of concrete production, it suffers from several significant limitations.\|[0008] The use of algae powder alone in the manner disclosed by LEE fails to fully leverage the carbon sequestration potential of marine algae, as it does not provide optimal surface area for CO2 absorption or create the necessary conditions for long-term carbon mineralization. Furthermore, simply mixing algae powder into concrete does not facilitate the formation of a matrix across the concrete surface that could enhance long-term sequestration and improve durability. There is a need for an innovative approach that can dramatically increase the CO2 absorption capacity of concrete, create synergistic interactions with other concrete components, and provide a mechanism for moisture retention to facilitate greater direct air capture of CO2. Such an approach would overcome the limitations of current algae-based concrete technologies and offer superior CO2 sequestration capabilities, enhanced durability, and improved overall performance.\|[0009] The need for carbon-capturing concrete has become increasingly urgent as the construction industry seeks to reduce its significant carbon footprint. To incentivize the adoption of such environmentally beneficial technologies, various tax credits and incentives have been established. Section 45Q of the Internal Revenue Code provides tax credits for carbon oxide sequestration, which can result in substantial savings for concrete producers utilizing this technology. Additionally, the Investment Tax Credit offers up to 30% credit on capital investments in carbon-capturing technologies. Other applicable incentives include R&D tax credits, Production Tax Credits, and various federal and state tax incentives designed to promote sustainable construction practices. These financial incentives not only make the adoption of carbon-sequestering concrete more economically viable but also align with broader policy goals of reducing greenhouse gas emissions and promoting sustainable development in the construction industry.\|[0010] These limitations result in a concrete composition that, while attempting to address environmental concerns, falls short of achieving significant and long-lasting carbon sequestration. The present invention seeks to overcome these limitations by providing a novel carbon-absorbing concrete composition and method of production that offers superior CO2 sequestration capabilities, enhanced durability, and improved overall performance compared to existing technologies.\|SUMMARY OF THE INVENTION\|[0011] The present invention relates to a carbon-sequestering concrete composition and method of production that addresses the limitations of previous approaches to reducing the carbon footprint of concrete.\|[0012] At the core of the preferred embodiment is the utilization of brown algae species, particularly “Macrocystis pyrifera”, which are transformed into alginate beads through a process called ionic gelation. These alginate beads dramatically increase the surface area available for CO2 absorption, forming a matrix across the concrete surface that enhances long-term sequestration and improves durability.\|[0013] The alginate beads are created through ionic gelation using brown algae powder. This process involves mixing the algae powder with water to create an alginate solution, which is then introduced dropwise into a bath containing calcium ions. As the droplets come into contact with the calcium ions, they undergo rapid gelation, forming stable, three-dimensional network structures with a high surface area, ideal for CO2 absorption and moisture retention in concrete.\|[0014] The preferred embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0015] The alginate beads play a crucial role in moisture retention in the context of the preferred embodiment, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0016] The preferred embodiment also addresses the formation of bicarbonate (HCO3-) ions in the presence of moisture from alginate beads, which is crucial for the carbon sequestration mechanism of the concrete. This process contributes to the concrete's ability to sequester CO2 not only during the initial curing phase but also throughout its service life.\|[0017] Furthermore, the alginate beads contribute to the self-healing of micro-cracks in the concrete, extending its lifespan and durability. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0018] In summary, the preferred embodiment provides a concrete composition with superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. It addresses the limitations of previous approaches and represents a significant advancement in sustainable construction materials.\|(US20250250199)\|BRIEF DESCRIPTION OF THE FIGURES\|[0019] FIG. 1 depicts the usage of an embodiment of the invention in association with a sidewalk.\|[0020] FIG. 2 depicts the usage of an embodiment of the invention in association with a pillar associated with a typical construction project.\|(US20250250199)\|DETAILED DESCRIPTION\|[0021] The preferred embodiment comprises a carbon-sequestering concrete and the associated methods of manufacture, addressing the limitations of previous methods and significantly enhancing CO2 absorption capabilities.\|[0022] At the core of this embodiment is the utilization of brown algae species, particularly “Macrocystis pyrifera”, which are transformed into alginate beads through a process called ionic gelation. These alginate beads dramatically increase the surface area available for CO2 absorption, forming a matrix across the concrete surface that enhances long-term sequestration and improves durability. The alginate beads in the preferred embodiment are created through a process called ionic gelation using brown algae powder, particularly from species “Macrocystis pyrifera”. This process is critical for enhancing CO2 absorption in the concrete mixture.\|[0023] The brown algae species “Macrocystis pyrifera” was chosen for creating alginate beads in the preferred embodiment due to its superior carbon sequestration capabilities. This species has evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions, making it significantly more effective for CO2 absorption compared to red and green algae species. The alginate extracted from Macrocystis pyrifera is particularly rich in carboxyl groups, which are crucial for the ionic gelation process used to form the beads. When mixed with water and introduced dropwise into a calcium ion bath, the alginate from Macrocystis pyrifera forms stable, three-dimensional network structures with a high surface area, ideal for CO2 absorption and moisture retention in concrete. In alternative embodiments, other brown algae species may serve as a substitute, including but not limited to Laminaria, Ascophyllum, Sargassum, and Fucus species. These alternative species also possess similar cell wall structures and carbon-binding capabilities, although Macrocystis pyrifera remains the preferred choice due to its particularly high alginate content and optimal gelation properties for concrete applications.\|[0024] To form the alginate beads, the brown algae powder is first mixed with water to create an alginate solution. This solution contains the alginate polymers naturally present in the cell walls of brown algae, which are rich in carboxyl groups.\|[0025] The alginate solution in an embodiment is then introduced dropwise into a bath containing divalent cations, typically calcium ions. As the alginate droplets come into contact with the calcium ions, they undergo a rapid gelation process. The calcium ions crosslink the alginate polymers, forming a stable, three-dimensional network structure. This ionic gelation process results in the formation of spherical alginate beads with a significantly increased surface area compared to the original algae powder. The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture. The ionic gelation process for forming alginate beads in an embodiment begins with mixing brown algae powder, particularly from species like “Macrocystis pyrifera”, with water to create an alginate solution. This solution contains the alginate polymers naturally present in the cell walls of brown algae, which are rich in carboxyl groups. The alginate solution is then introduced dropwise into a bath containing divalent cations, typically calcium ions. As the alginate droplets come into contact with the calcium ions, they undergo a rapid gelation process. The calcium ions crosslink the alginate polymers, forming a stable, three-dimensional network structure. This process results in the formation of spherical alginate beads with a significantly increased surface area compared to the original algae powder. The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture. The size and density of the alginate beads can be controlled by adjusting various parameters during the gelation process, such as the concentration of the alginate solution, the type and concentration of the crosslinking ions, and the droplet size. This allows for optimization of the beads' properties to suit the specific requirements of the concrete mixture. Once formed, the alginate beads are collected and may undergo further processing, such as washing to remove excess ions and drying to a desired moisture content. The resulting beads are then ready to be incorporated into the concrete mixture, where they will play a crucial role in enhancing CO2 sequestration and improving the overall performance of the concrete in accordance with an embodiment of the invention.\|[0026] The size and density of the alginate beads can be controlled by adjusting various parameters during the gelation process, such as the concentration of the alginate solution, the type and concentration of the crosslinking ions, and the droplet size. This allows for optimization of the beads' properties to suit the specific requirements of the concrete mixture.\|[0027] Once formed, the alginate beads are collected and may undergo further processing, such as washing to remove excess ions and drying to a desired moisture content. The resulting beads are then ready to be incorporated into the concrete mixture, where they will play a crucial role in enhancing CO2 sequestration and improving the overall performance of the concrete.\|[0028] The formation of these alginate beads through ionic gelation is a key innovation that sets the preferred embodiment of the invention apart from previous approaches that simply mixed algae powder into concrete. The beads provide a matrix across the surface of the concrete, dramatically enhancing long-term sequestration and improving the concrete's durability.\|[0029] The alginate beads formed from brown algae powder significantly increase the CO2 absorption surface area compared to simply using algae powder in concrete. This enhancement in surface area is achieved through the ionic gelation process, which creates a porous, three-dimensional structure within each bead.\|[0030] When algae powder is directly mixed into concrete in accordance with the preferred embodiment, it remains as discrete particles with limited surface area exposed for CO2 interaction. In contrast, the alginate beads form a matrix across the surface of the concrete, dramatically increasing the total surface area available for carbon dioxide absorption.\|[0031] The ionic gelation process creates a network of interconnected pores within each alginate bead. This porous structure allows CO2 molecules to penetrate deep into the bead, rather than just interacting with the outer surface. As a result, the effective surface area for CO2 absorption is multiplied many times over compared to solid algae powder particles in accordance with the preferred embodiment.\|[0032] Furthermore, the alginate beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. This moisture retention further enhances CO2 absorption, as the carbonation process reacts more readily in the presence of water. The combination of increased surface area and moisture retention allows for significantly more efficient CO2 capture and conversion to stable carbonate compounds.\|[0033] The size and density of the alginate beads can be controlled during the gelation process in accordance with various embodiments, allowing for optimization of the surface area to volume ratio. By adjusting parameters such as alginate concentration, crosslinking ion type and concentration, and droplet size, the beads can be tailored to maximize their CO2 absorption capacity.\|[0034] Additionally, the alginate beads create a more uniform distribution of CO2 absorption sites throughout the concrete matrix compared to algae powder. This even distribution ensures that the carbon sequestration potential is maximized across the entire concrete structure, rather than being limited to localized areas where algae powder particles might cluster.\|[0035] The cumulative effect of these factors in accordance with the preferred embodiment-increased surface area, porous structure, moisture retention, and uniform distribution-results in CO2 absorption capabilities that are orders of magnitude greater than what can be achieved with simple algae powder incorporation associated with other attempts. This dramatic enhancement in carbon sequestration efficiency is a critical innovation of the preferred embodiment of the invention, enabling concrete structures to serve as highly effective carbon sinks throughout their service life.\|[0036] The preferred embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS).\|[0037] These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption. The alginate beads also play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2.\|[0038] The preferred embodiment enhances pozzolanic reactions through the synergistic interaction between alginate beads and various components of the concrete mix, particularly fly ash and metakaolin.\|[0039] Pozzolanic reactions occur when siliceous or aluminosiliceous materials react with calcium hydroxide in the presence of water to form compounds with cementitious properties. In the context of this invention, the alginate beads create localized high-humidity environments within the concrete matrix, which facilitates these reactions. The increased moisture content provided by the beads promotes the dissolution of silica and alumina from the pozzolanic materials, allowing them to react more readily with calcium hydroxide produced during the hydration of cement or geopolymer precursors. This enhanced reactivity leads to the formation of additional calcium silicate hydrate (C—S—H) and calcium aluminate hydrate (C-A-H) gels, which contribute to the concrete's strength and durability. Furthermore, the pozzolanic reactions consume calcium hydroxide, reducing the concrete's susceptibility to chemical attacks and improving its long-term performance. The increased pozzolanic activity also creates more sites for carbon dioxide capture within the concrete composition, as the newly formed C—S—H and C-A-H gels provide additional surface area for CO2 absorption and carbonation.\|[0040] The preferred embodiment creates additional sites for carbon dioxide capture through several mechanisms. The alginate beads formed from brown algae powder increase the surface area available for CO2 absorption, creating a matrix across the concrete surface that enhances long-term sequestration. This matrix structure provides numerous additional sites for CO2 to interact with and be captured by the concrete. Furthermore, the synergistic interactions between the alginate beads and other concrete components, such as fly ash and ground granulated blast furnace slag (GGBFS), lead to enhanced pozzolanic reactions in association with the preferred embodiment.\|[0041] These reactions create more sites in the concrete composition specifically for capturing carbon dioxide. The increased pozzolanic activity results in the formation of additional calcium silicate hydrate (C—S—H) and calcium aluminate hydrate (C-A-H) gels, which provide extra surface area for CO2 absorption and carbonation. The alginate beads also interact positively with other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4).\|[0042] The alginate beads in the preferred embodiment interact synergistically with additives like magnesium carbonate and olivine (Mg2SiO4) to enhance the concrete's CO2 sequestration capabilities. The moisture retention properties of the alginate beads play a crucial role in facilitating these interactions.\|[0043] For magnesium carbonate, the localized high-humidity environments created by the alginate beads promote its gradual dissolution within the concrete matrix. This dissolution process releases magnesium ions, which can then react with dissolved CO2 to form stable magnesium carbonate compounds, effectively capturing and storing atmospheric carbon dioxide.\|[0044] In the case of olivine (Mg2SiO4), the humidity retained by the alginate beads creates conditions favorable for its dissolution in accordance with the preferred embodiment. As the olivine dissolves, it releases magnesium ions into the concrete matrix. These magnesium ions can then interact with the alginate structure, enhancing the formation of magnesium carbonates. This process not only contributes to additional CO2 sequestration but also improves the overall strength and durability of the concrete.\|[0045] The alginate beads create “localized high-humidity environments” within the concrete through their unique moisture absorption and retention properties. When incorporated into the concrete mixture, these beads absorb and hold water, acting as microscopic reservoirs distributed throughout the concrete matrix.\|[0046] In accordance with the preferred embodiment, as the concrete cures and ages, the alginate beads continue to retain this moisture, creating small pockets of high humidity surrounding each bead. These localized high-humidity environments are crucial for facilitating CO2 absorption, as the carbonation process reacts more readily in the presence of water. The retained moisture provides a medium for atmospheric CO2 to dissolve, forming carbonic acid which then interacts with calcium ions to produce stable calcium carbonate. This process of CO2 absorption and carbonate formation is significantly enhanced by the consistent availability of moisture provided by the alginate beads, allowing for continuous carbon sequestration throughout the concrete's service life. Furthermore, these high-humidity microenvironments promote the gradual dissolution of other additives like magnesium carbonate and olivine, further enhancing the concrete's overall CO2 absorption capacity.\|[0047] The continuous moisture provision by the alginate beads ensures that these reactions can occur over an extended period, prolonging the concrete's carbon capture capabilities. As atmospheric CO2 dissolves in the water retained by the beads, it forms carbonic acid, which then reacts with the magnesium ions released from both magnesium carbonate and olivine to produce stable carbonate compounds. These interactions between the alginate beads and additives like magnesium carbonate and olivine create a self-sustaining cycle of CO2 absorption and mineralization within the concrete. The process continues throughout the concrete's service life, significantly enhancing its long-term carbon sequestration potential compared to traditional concrete compositions.\|[0048] The preferred embodiment prolongs the period of CO2 absorption through several innovative mechanisms. The alginate beads formed from brown algae powder play a crucial role in extending the carbon sequestration capabilities of the concrete over time. These beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix that facilitate ongoing CO2 absorption.\|[0049] The synergistic interactions between the alginate beads and other concrete components, such as ground granulated blast furnace slag (GGBFS), increase both the hydration and carbonation processes. This effectively extends the duration during which the concrete can actively absorb carbon dioxide from the atmosphere.\|[0050] Furthermore, the alginate beads enhance the CO2 sequestration capabilities of other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4). The humidity retained by the beads creates conditions that promote the gradual dissolution of these minerals, leading to sustained carbon capture over an extended period. The continuous process of CO2 absorption is supported by the ongoing formation of carbonate compounds within the concrete matrix.\|[0051] The alginate beads facilitate the dissolution of minerals including olivine (Mg2SiO4) to enhance carbon capture through several mechanisms. The beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. This increased moisture content promotes the gradual dissolution of olivine, releasing magnesium ions into the surrounding concrete. The humidity in the alginate beads creates these localized high moisture environments, which are crucial for facilitating olivine dissolution. As the olivine dissolves, the released magnesium ions interact with the alginate structure, enhancing the formation of magnesium carbonates. This process not only contributes to additional CO2 sequestration but also improves the overall strength and durability of the concrete. The continuous moisture provision by the alginate beads ensures that these reactions can occur over an extended period, prolonging the concrete's carbon capture capabilities. Furthermore, the beads provide additional surface area for basalt dissolution, which leads to further carbon capture. This synergistic interaction between the alginate beads and olivine creates a self-sustaining cycle of CO2 absorption and mineralization within the concrete, significantly enhancing its long-term carbon sequestration potential compared to traditional concrete compositions.\|[0052] As atmospheric CO2 dissolves in the water retained by the alginate beads, it forms carbonic acid, which then reacts with calcium ions to produce stable calcium carbonate. This cycle of absorption and mineralization continues throughout the concrete's service life, significantly prolonging its CO2 sequestration capabilities.\|[0053] Additionally, the formation of stable calcium carbonate contributes to the self-healing of micro-cracks in the concrete. This self-healing property not only extends the overall lifespan of the concrete but also maintains its ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure. The alginate beads also contribute to the self-healing of micro-cracks in the concrete through several mechanisms. As the concrete cures and ages, the alginate beads continue to absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. When micro-cracks form, these moist environments facilitate the ongoing formation of carbonate compounds. As atmospheric CO2 dissolves in the water retained by the alginate beads, it forms carbonic acid, which then reacts with calcium ions to produce stable calcium carbonate. This calcium carbonate precipitates within the micro-cracks, gradually filling them and restoring the concrete's integrity. The continuous nature of this process, enabled by the moisture-retaining properties of the alginate beads, allows for ongoing self-healing throughout the concrete's service life. Additionally, the alginate beads' ability to enhance pozzolanic reactions and create additional sites for carbon dioxide capture contributes to the formation of supplementary binding materials that can further aid in crack repair. This self-healing property not only extends the overall lifespan of the concrete but also maintains its ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0054] By incorporating these innovative features, the preferred embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0055] The humidity retained by the alginate beads creates localized high moisture environments that facilitate the dissolution of these minerals, leading to further carbon capture opportunities. This process increases the overall number of sites available for CO2 sequestration within the concrete matrix. Lastly, the moisture retention properties of the alginate beads create conditions favorable for the ongoing formation of carbonate compounds throughout the concrete.\|[0056] As CO2 dissolves in the water absorbed by the beads, it forms carbonic acid, which then interacts with calcium ions to form stable calcium carbonate. This continuous process effectively creates new sites for carbon dioxide capture as the concrete ages, prolonging its CO2 sequestration capabilities over time.\|[0057] This innovative concrete composition not only reduces the carbon footprint associated with production but also actively removes CO2 from the atmosphere throughout its service life. The carbon capture process in the preferred embodiment occurs strongly over the initial approximately 60 days due to the rapid initial reactions between the alginate beads and atmospheric CO2, but continues on a smaller scale for many years thereafter.\|[0058] This prolonged sequestration is enabled by several key mechanisms:\|[0059] During the initial curing period, the alginate beads formed through ionic gelation provide a large surface area for CO2 absorption, allowing for rapid carbonation reactions. The beads absorb and retain moisture, creating localized high-humidity environments that facilitate the dissolution of CO2 and its reaction with calcium ions to form stable calcium carbonate.\|[0060] As the concrete continues to age, the synergistic interactions between the alginate beads and other components of the mix, such as ground granulated blast furnace slag (GGBFS) and fly ash, sustain the carbon capture process. These interactions lead to ongoing pozzolanic reactions and the creation of additional sites for CO2 absorption, albeit at a slower rate than during the initial curing period.\|[0061] The moisture retention properties of the alginate beads play a crucial role in maintaining conditions favorable for long-term CO2 sequestration. Even as the concrete ages, the beads continue to absorb and retain water from the environment, providing a medium for CO2 to dissolve and react with available calcium ions.\|[0062] Furthermore, the formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete. This self-healing process not only extends the lifespan of the concrete but also maintains pathways for continued CO2 absorption over many years.\|[0063] The gradual dissolution of minerals such as magnesium carbonate and olivine, facilitated by the moisture retained in the alginate beads, provides a slow but steady source of reactive components for ongoing CO2 sequestration. This process continues at a reduced rate long after the initial curing period, allowing the concrete to capture carbon dioxide from the atmosphere throughout its service life.\|[0064] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions in the alginate beads contributes to the self-healing of micro-cracks, further extending the concrete's lifespan and durability. By addressing the limitations of previous approaches, this invention represents a significant advancement in sustainable construction materials, offering superior carbon sequestration capabilities, enhanced durability, and improved overall performance.\|[0065] The preferred embodiment of the present invention addresses the limitations of previous approaches by utilizing brown algae species, particularly “Macrocystis pyrifera”, which have evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions. This makes them significantly more effective for CO2 absorption compared to red and green algae species. The use of brown algae provides a more efficient and targeted approach to carbon sequestration in concrete, leveraging their natural adaptations to marine environments.\|[0066] A critical innovation in the preferred embodiment is the formation of alginate beads using brown algae powder through a process called ionic gelation. This process dramatically increases the surface area available for CO2 absorption, enhancing it by orders of magnitude compared to simply mixing algae powder into the concrete. The alginate beads form a matrix across the surface of the concrete, which significantly enhances long-term sequestration and improves the concrete's durability. This matrix structure allows for more uniform and efficient carbon dioxide capture throughout the concrete, leading to superior performance over extended periods.\|[0067] The formation of alginate beads offers several key advantages over traditional methods. The increased surface area provided by the beads allows for more efficient CO2 absorption, while also promoting the formation of more stable calcium carbonate. This stability is crucial for long-term carbon sequestration, ensuring that the captured CO2 remains locked within the concrete structure for extended periods. Additionally, the uniform distribution of alginate beads throughout the concrete mix ensures that the CO2 capture potential is evenly spread, maximizing the overall sequestration capacity of the concrete.\|[0068] The alginate beads in the preferred embodiment interact synergistically with other components of the concrete mix, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance the overall performance and carbon sequestration capabilities of the concrete. For instance, the presence of alginate beads leads to enhanced pozzolanic reactions with fly ash, creating more sites within the concrete composition for capturing carbon dioxide. This increased reactivity not only improves the concrete's strength but also its ability to absorb CO2 over time.\|[0069] In the case of GGBFS, the alginate beads increase both the hydration and carbonation processes, effectively prolonging the period during which the concrete can absorb carbon dioxide. This extended absorption window is crucial for maximizing the total amount of CO2 sequestered over the lifetime of the concrete structure. Similarly, the interaction between alginate beads and metakaolin results in increased pozzolanic activity, further enhancing the concrete's performance and carbon capture capabilities.\|[0070] The alginate beads also enhance the CO2 sequestration capabilities of other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4). The beads create localized high-moisture environments that facilitate the dissolution of these minerals, leading to increased formation of carbonate compounds. This synergistic effect amplifies the overall carbon sequestration potential of the concrete, making it significantly more effective at reducing atmospheric CO2 levels compared to traditional concrete formulations.\|[0071] One of the most crucial roles played by the alginate beads in the preferred embodiment is in moisture retention, which is essential for the carbon sequestration process. The beads absorb and retain water, creating localized high-humidity environments within the concrete matrix. This increased moisture content is vital for facilitating greater direct air capture (DAC) of CO2, as the carbonation process reacts more readily in the presence of water. The absorbed water acts as a medium in which CO2 can dissolve, forming carbonic acid (H2CO3) and initiating a series of chemical reactions that lead to carbon sequestration.\|[0072] The presence of moisture within the alginate beads creates conditions favorable for the formation of bicarbonate (HCO3-) ions. This process is fundamental to the sequestration of various compounds within the concrete matrix. As CO2 dissolves and forms carbonic acid, it interacts with the calcium ions present within the alginate beads. This interaction leads to the formation of stable calcium carbonate, effectively locking the captured CO2 into the concrete structure. This process not only increases the overall CO2 uptake but also contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability.\|[0073] The formation of bicarbonate (HCO3-) ions in the presence of moisture from alginate beads is a crucial process in the carbon sequestration mechanism of the concrete. The alginate beads, which are rich in carboxyl groups, absorb and retain water, creating localized high-humidity environments within the concrete matrix. As atmospheric CO2 dissolves in this water, it forms carbonic acid (H2CO3). In the presence of moisture, the carboxyl groups in the alginate react with this carbonic acid, leading to the formation of bicarbonate (HCO3-) ions.\|[0074] This process is critical in accordance with the preferred embodiment because the bicarbonate ions serve as an intermediate step in the overall carbon mineralization process. The bicarbonate ions can further react with calcium ions within the alginate beads or from other sources in the concrete to form stable calcium carbonate (CaCO3). This reaction sequence effectively locks in the absorbed CO2, converting it from a gaseous form to a solid, stable mineral form within the concrete structure. The continuous moisture provision by the alginate beads ensures that this bicarbonate formation process can occur over an extended period, prolonging the concrete's carbon capture capabilities. This ongoing process contributes to the concrete's ability to sequester CO2 not only during the initial curing phase but also throughout its service life, albeit at a slower rate in later stages.\|[0075] An embodiment of the present invention comprises a carbon-sequestering concrete composition with specific components and their respective percentages by mass. Alternative embodiments deviate slightly from the specific percentages by mass presented in the foregoing.\|[0076] The composition includes Fly Ash (Class F) at 25%, which serves as the primary binder and significantly reduces CO2 emissions compared to traditional cement. This component allows for increased CO2-reactive materials in the mixture, enhancing the overall carbon sequestration potential of the concrete.\|[0077] Ground Granulated Blast Furnace Slag (GGBFS) constitutes 20% of the mixture. This component enhances the strength and durability of the concrete while acting as a supplementary binder. The inclusion of GGBFS contributes to the reduction of the carbon footprint associated with concrete production by partially replacing traditional cement.\|[0078] Metakaolin, comprising 5% of the mixture, improves early strength and reduces permeability of the concrete. This component allows room for more CO2 capture materials, further enhancing the carbon sequestration capabilities of the concrete. The inclusion of metakaolin also contributes to the overall sustainability of the mixture by reducing the need for energy-intensive cement production.\|[0079] Recycled Aggregates make up 20% of the composition, while Natural Aggregates constitute 15%. The use of recycled aggregates significantly reduces the environmental impact of the concrete production process by minimizing the need for new raw materials extraction. Natural aggregates provide the necessary mechanical strength to the concrete. The balance between recycled and natural aggregates is carefully optimized to maintain the structural integrity of the concrete while maximizing its sustainability.\|[0080] Silica Fume, at 2% of the mixture, fills micro-pores and enhances the strength and durability of the concrete. This component improves the overall pore structure of the concrete, which is crucial for both strength development and carbon sequestration potential. The fine particles of silica fume react with calcium hydroxide produced during cement hydration, forming additional calcium silicate hydrate (C—S—H) gel, which enhances the concrete's properties.\|[0081] Sodium Hydroxide (NaOH) and Sodium Silicate (Na2SiO3) serve as activators for the geopolymerization process, constituting 1.5% and 2.5% of the mixture respectively. These components are essential for activating the aluminosilicate materials in the mixture, particularly the fly ash and GGBFS. The careful balance of these activators ensures optimal reaction efficiency while minimizing environmental impact.\|[0082] Algae Biomass, used for creating alginate beads, makes up 2% of the mixture. This component is crucial for maximizing CO2 sequestration potential through the formation of alginate beads and direct air capture. The algae biomass is transformed into alginate beads through a process called ionic gelation, which dramatically increases the surface area available for CO2 absorption.\|[0083] Calcium Carbonate (CaCO3) and Magnesium Carbonate (MgCO3) each constitute 2% of the mixture. These components enhance carbonation during curing and beyond, improving overall CO2 capture. They react with CO2 to form stable carbonate compounds, effectively sequestering carbon within the concrete structure.\|[0084] Silica from Algae, comprising 1% of the mixture, serves as a sustainable silica source that improves strength with minimal environmental impact. This component contributes to the overall sustainability of the concrete mixture while enhancing its mechanical properties.\|[0085] Magnesium Silicate and Olivine (finely ground) each make up 1% of the mixture. These components enhance CO2 sequestration through mineral carbonation. The fine grinding of olivine increases its surface area, making it more reactive and efficient in capturing CO2. These materials react with atmospheric CO2 to form stable carbonate minerals, effectively locking away carbon for long periods.\|[0086] Basalt Rock Dust, constituting 1% of the mixture, provides trace minerals and enhances CO2 uptake through mineral carbonation. This component contributes to the overall carbon sequestration potential of the concrete while also improving its mechanical properties.\|[0087] Biochar (Activated) makes up 1% of the mixture. This component sequesters carbon and improves internal curing of the concrete. Biochar's porous structure allows it to absorb and retain CO2, contributing significantly to the overall carbon sequestration capabilities of the concrete.\|[0088] Alginate Beads, maximized at 1.5% of the mixture, play a crucial role in enhancing CO2 capture. These beads, formed through ionic gelation of brown algae powder, dramatically increase the surface area available for CO2 absorption. They form a matrix across the concrete surface, significantly enhancing long-term sequestration and improving durability.\|[0089] Carbonation Accelerators (C—S—H Seeds) constitute 1.5% of the mixture. These accelerate strength gain and CO2 uptake during curing. The C—S—H seeds provide nucleation sites for the formation of additional calcium silicate hydrate gel, which not only enhances the concrete's strength but also increases its capacity to absorb CO2.\|[0090] Water, making up 1% of the mixture, is necessary for workability and chemical reactions. The water content is carefully controlled to ensure optimal hydration of cementitious materials and proper workability of the concrete mix, while also facilitating the various chemical reactions involved in CO2 sequestration.\|[0091] This embodiment of the carbon-sequestering concrete composition demonstrates superior carbon sequestration capabilities compared to conventional concrete. For every 1,000 tons of concrete produced, this embodiment emits 81.4 tons of CO2 but sequesters 91.25 tons of CO2, resulting in a net sequestration of 9.85 tons of CO2. This represents a total reduction of 909.85 tons of CO2 per 1,000 tons produced, or a 101.1% reduction compared to conventional concrete.\|[0092] The CO2 sequestration in this embodiment occurs through several mechanisms, including biochar absorption, algae biomass uptake, carbonates reaction, mineral carbonation, alginate bead absorption, and CO2 absorption during curing. The total CO2 sequestered amounts to 91,250 kg (91.25 tonnes) per 1,000 tons of concrete produced.\|[0093] The carbon-sequestering concrete composition described in this embodiment demonstrates remarkable carbon sequestration capabilities that significantly outperform conventional concrete. For every 1,000 tons of concrete produced, this innovative composition achieves a net carbon sequestration of 9.85 tons of CO2, in stark contrast to conventional concrete which emits approximately 900 tons of CO2 for the same amount produced. This results in a total reduction of 909.85 tons of CO2 per 1,000 tons produced, representing a 101.1% reduction compared to conventional concrete.\|[0094] The superior carbon sequestration performance of this concrete composition is achieved through a combination of reduced emissions during production and active carbon capture mechanisms. While the embodiment emits 81.4 tons of CO2 during production, it sequesters 91.25 tons of CO2, resulting in the net negative carbon footprint. This remarkable feat is accomplished through several key mechanisms that work synergistically to capture and store carbon dioxide.\|[0095] The CO2 sequestration in this embodiment occurs through several primary mechanisms, including the following: Biochar absorption, which accounts for 29,333 kg of CO2 sequestered. The activated biochar in the mixture acts as a highly effective carbon sink due to its porous structure and high surface area. Algae Biomass uptake, responsible for sequestering 36,667 kg of CO2. The algae biomass, particularly when transformed into alginate beads, provides a substantial contribution to the overall carbon capture capacity of the concrete. Carbonates Reaction, which sequesters 2,000 kg of CO2. This involves the reaction of CO2 with calcium and magnesium carbonates present in the mixture, forming stable carbonate compounds. Mineral Carbonation, accounting for 2,500 kg of CO2 sequestered. This process involves the reaction of CO2 with minerals such as magnesium silicate and olivine to form stable carbonate minerals. Alginate Beads, which directly capture 750 kg of CO2 but also play a crucial role in enhancing the capture efficiency of other materials. The alginate beads, formed through ionic gelation of brown algae powder, create a matrix across the concrete surface that significantly increases the surface area available for CO2 absorption. CO2 absorbed during curing, which accounts for 20,000 kg of the total CO2 sequestered. This substantial amount is captured during the initial setting and hardening phase of the concrete.\|[0096] These mechanisms in an embodiment collectively result in a total CO2 sequestration of 91,250 kg (91.25 tonnes) per 1,000 tons of concrete produced. The synergistic interactions between the various components, particularly the alginate beads and other concrete constituents like geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS), enhance pozzolanic reactions and create additional sites for carbon dioxide capture. Furthermore, the moisture retention properties of the alginate beads create localized high-humidity environments within the concrete, facilitating greater direct air capture of CO2 throughout the concrete's service life.\|[0097] This innovative concrete composition not only addresses the carbon emissions associated with concrete production but also actively removes CO2 from the atmosphere, representing a significant advancement in sustainable construction materials.\|[0098] This embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0099] The alginate beads, formed through ionic gelation of brown algae powder, play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0100] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0101] By incorporating these innovative features, this embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0102] An alternative embodiment of the present invention comprises a carbon-sequestering concrete composition with the following components and their respective percentages by mass\| - Fly Ash (Class F): 22%\| - Ground Granulated Blast Furnace Slag (GGBFS): 20%\| - Metakaolin: 4%\| - Recycled Aggregates: 20%\| - Natural Aggregates: 12%\| - Silica Fume: 3%\| - Sodium Hydroxide (NaOH): 1%\| - Sodium Silicate (Na2SiO3): 2%\| - Algae Biomass (for Beads): 3%\| - Calcium Carbonate (CaCO3): 3%\| - Magnesium Carbonate (MgCO3): 3%\| - Silica from Algae: 1%\| - Magnesium Silicate: 2%\| - Olivine (Finely Ground): 3%\| - Basalt Rock Dust: 2%\| - Biochar (Activated): 2%\| - Alginate Beads (Maximized): 3%\| - Carbonation Accelerators (C—S—H Seeds): 2%\| - Water: 1%\|[0122] In this alternative embodiment, the Fly Ash (Class F) content is reduced to 22% in such embodiment to allow for increased CO2-reactive materials. This adjustment maintains the primary binding function while enhancing the overall carbon sequestration potential of the concrete. The Ground Granulated Blast Furnace Slag (GGBFS) in such embodiment is included at 20%, continuing to enhance strength and durability while acting as a supplementary binder. This component contributes significantly to reducing the carbon footprint associated with concrete production. Metakaolin is reduced to 4% in such embodiment, still improving early strength and reducing permeability while allowing for more CO2 capture materials. This adjustment contributes to the overall sustainability of the mixture. The ratio of Recycled Aggregates to Natural Aggregates is adjusted to 20% and 12% respectively in accordance with such embodiment. This change further reduces the environmental impact of the concrete production process while maintaining necessary mechanical strength. Silica Fume is increased to 3% to enhance the pore structure, strength, and durability of the concrete. This increase improves the overall performance and CO2 sequestration potential. The activators, Sodium Hydroxide (NaOH) and Sodium Silicate (Na2SiO3), are adjusted to 1% and 2% respectively. This optimization balances the geopolymerization process while minimizing environmental impact. Algae Biomass for beads is increased to 3%, maximizing CO2 sequestration potential through enhanced alginate bead formation and direct air capture. Both Calcium Carbonate (CaCO3) and Magnesium Carbonate (MgCO3) are increased to 3% each in accordance with this embodiment, enhancing carbonation during curing and beyond, thus improving overall CO2 capture. Magnesium Silicate is increased to 2%, and Olivine (Finely Ground) to 3%, enhancing CO2 sequestration through increased mineral carbonation potential. Basalt Rock Dust is increased to 2%, providing more trace minerals and enhancing CO2 uptake through mineral carbonation. Biochar (Activated) is increased to 2%, improving carbon sequestration and internal curing of the concrete. Alginate Beads are included at 3% in accordance with such embodiment, significantly enhancing CO2 capture and improving the concrete's overall performance. Carbonation Accelerators (C—S—H Seeds) are increased to 2%, further accelerating strength gain and CO2 uptake during curing. Water content remains at 1%, maintaining the necessary workability and facilitating chemical reactions.\|[0123] This alternative embodiment demonstrates enhanced carbon sequestration capabilities. For every 1,000 tons of concrete produced, this embodiment creates approximately 64.2 tons of CO2 but sequesters 101 tons of CO2 through direct air capture (DAC) and mineralization. This results in a net sequestration of approximately 36.8 tons of CO2 per 1,000 tons of concrete produced in accordance with an exemplary implementation.\|[0124] The carbon sequestration in this embodiment occurs through several mechanisms, including biochar absorption, algae biomass uptake, carbonates reaction, mineral carbonation, alginate bead absorption, and CO2 absorption during curing. The total CO2 sequestered amounts to 101,000 kg (101 tonnes) per 1,000 tons of concrete produced.\|[0125] This embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0126] The alginate beads, formed through ionic gelation of brown algae powder, play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0127] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability in an embodiment. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0128] By incorporating these innovative features and optimizing the component ratios, this alternative embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0129] The carbon-sequestering concrete composition described in the embodiments of the invention in an example is designed to maximize eligibility for significant tax credits and incentives, potentially resulting in substantial cost savings for concrete producers and users. In an example, the tax credits could be allocated for 1,000 tons of concrete produced as an embodiment of the invention in accordance with the following:\|[0130] Section 45Q tax credits could provide approximately $100,000 to $150,000 in savings per 1,000 tons of concrete produced, depending on the final determination by the EPA/IRS and the results of a Life Cycle Assessment (LCA). This estimate is based on the net carbon sequestration capabilities of the concrete, which ranges from 9.85 to 36.8 tons of CO2 per 1,000 tons of concrete produced, depending on the specific embodiment.\|[0131] The Investment Tax Credit could cover up to 30% of a concrete mixer's investment in this carbon-sequestering concrete technology. This credit would apply to the capital expenditures required to implement the new production methods and equipment necessary for manufacturing this innovative concrete.\|[0132] Additional tax incentives that may be applicable in association with and as an expected benefit of an embodiment of the invention include:\|[0133] R&D tax credits for the ongoing development and improvement of the carbon-sequestering concrete technology. Production Tax Credits for the manufacture of environmentally beneficial products. Various federal and state tax incentives designed to promote sustainable construction practices and materials.\|[0134] When considering a larger scale of production, for example 20 medium sized building construction projects, the total savings from these combined tax credits and incentives could exceed $5 million for a concrete producer. This estimate takes into account the cumulative effect of the various tax benefits across multiple projects.\|[0135] The economic benefits of these tax credits extend beyond mere cost savings. They also enhance the competitiveness of the carbon-sequestering concrete in the market. Before applying any tax credits, the price of this innovative concrete is approximately $138 per ton, which is already competitive with conventional concrete. However, after factoring in the tax credits, the effective price drops to around $112 per ton, making it more economical than conventional concrete options.\|[0136] In accordance with various embodiments, the exact allocation and amount of tax credits may vary depending on factors such as the specific project details, the concrete producer's financial situation, and any changes in tax laws or regulations. Additionally, the realization of these tax benefits would likely require careful documentation of the carbon sequestration capabilities of the concrete, as well as compliance with relevant regulatory requirements, which is an intended use in accordance with an embodiment of the invention.\|[0137] Another embodiment of the invention comprises a carbon-sequestering concrete composition optimized for maximum CO2 sequestration and economic viability through tax incentives, as follows:\|[0138] The composition of this carbon-sequestering concrete in such embodiment is carefully formulated to maximize both CO2 sequestration capabilities and eligibility for tax credits. The mixture, designed for a 1,000-ton batch, comprises several key components that work synergistically to achieve these goals.\|[0139] Aluminosilicate materials form the foundation of the geopolymer binder system in such embodiment. These include 30% Fly Ash (Class F), 20% Ground Granulated Blast Furnace Slag (GGBFS), 5% Metakaolin, and 3% Silica Fume. These materials not only contribute to the strength and durability of the concrete but also play a crucial role in CO2 sequestration through pozzolanic reactions.\|[0140] A significant portion of the mix in such embodiment is dedicated to CO2-absorbing materials. This includes 15% Magnesium Silicate, 15% finely ground Olivine, 10% Activated Biochar, 3% Calcium Carbonate (CaCO3), and 2% Magnesium Carbonate (MgCO3). These components are specifically chosen for their high CO2 sequestration potential and their ability to form stable carbonate compounds over time.\|[0141] The aggregate portion of the mix consists of 10% Natural Aggregates and 5% Recycled Aggregates, balancing structural requirements with sustainability considerations in accordance with such embodiment. The alkaline activators, crucial for the geopolymerization process, include 2% Sodium Hydroxide (NaOH) and 4% Sodium Silicate (Na2SiO3).\|[0142] A key innovation in this embodiment is the incorporation of algae-derived components. This comprises 1% Silica from Algae, 3% Algae Biomass for bead formation, and 5% Alginate Beads. These components significantly enhance the CO2 sequestration capabilities of the concrete through increased surface area and the creation of localized high-humidity environments that facilitate CO2 absorption.\|[0143] The mixture in such embodiment also comprises 2% Carbonation Accelerators in the form of C—S—H Seeds, which enhance the rate of CO2 uptake during the curing process. The water content is maintained at 5%, with small amounts of superplasticizers (0.5%) and air-entraining agents (0.1%) added to optimize workability and durability.\|[0144] The production process of this concrete composition in such embodiment has been observed by the inventor to result in total emissions of 108,550 kg CO2 per 1,000 tons produced. However, the CO2 sequestration capabilities of the mixture are substantial, with a total CO2 sequestration potential of 435,000 kg CO2 per 1,000 tons of concrete. This results in a net negative carbon footprint of −326,450 kg CO2 per 1,000 tons of concrete produced in accordance with inventor observations.\|[0145] The CO2 sequestration occurs through several mechanisms in accordance with such embodiment. The Magnesium Silicate and Olivine each sequester 45,000 kg CO2. The Activated Biochar contributes significantly with 200,000 kg CO2 sequestered. The Algae Biomass and Alginate Beads together sequester 80,000 kg CO2. The Calcium and Magnesium Carbonates add another 5,000 kg CO2 to the total. Additionally, the CO2 curing process is estimated to sequester an additional 50,000 kg CO2.\|[0146] This embodiment is designed to maximize eligibility for tax credits, particularly the Section 45Q tax credit for carbon oxide sequestration. For every 1,000 tons of concrete produced, this composition is eligible for approximately $26,100 in Section 45Q tax credits. When combined with other available tax credits such as the Investment Tax Credit and R&D credits, the total tax credits per 1,000 tons could reach approximately $354,100 in accordance with the regulations in place as of September 2024.\|[0147] The economic viability of this concrete composition in such embodiment is further enhanced by these tax incentives. After accounting for all applicable tax credits, the effective cost of this concrete is estimated to be $57.85 per ton, making it highly competitive in the market.\|[0148] In comparison to other carbon-reducing concrete technologies, this embodiment demonstrates superior performance. For instance, when compared to Blue Planet's concrete, which sequesters 330 tons CO2 per 1,000 tons of concrete, this embodiment sequesters 435 tons CO2. This results in higher eligibility for Section 45Q tax credits and overall tax credits under applicable regulations in place in September 2024.\|[0149] The enhanced CO2 sequestration capabilities of this concrete composition in such embodiment are achieved through the synergistic interactions between its components, particularly the alginate beads and other concrete constituents like geopolymers, fly ash, and ground granulated blast furnace slag. These interactions enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The moisture retention properties of the alginate beads create localized high-humidity environments within the concrete, facilitating greater direct air capture of CO2 throughout the concrete's service life.\|[0150] This innovative concrete composition in accordance with such embodiment not only addresses the carbon emissions associated with concrete production but also actively removes CO2 from the atmosphere, representing a significant advancement in sustainable construction materials. Its superior carbon sequestration capabilities, combined with its economic viability through tax incentives, position it as a potentially disruptive technology in the concrete industry.\|[0151] The carbon-sequestering concrete composition described in the embodiment can be formulated with varying proportions of its key components to optimize performance and CO2 sequestration capabilities. The aluminosilicate materials, which form the foundation of the geopolymer binder system, can range from 30-60% of the total composition. This range allows for flexibility in adjusting the mix based on specific project requirements and material availability. The CO2-absorbing materials, crucial for the concrete's carbon sequestration properties, can constitute 30-50% of the mixture. This range ensures a significant portion of the concrete is dedicated to active CO2 absorption while maintaining structural integrity.\|[0152] The aggregate portion, balancing structural requirements with sustainability considerations, can range from 10-20% of the total composition in accordance with such embodiment. The alkaline activators, essential for the geopolymerization process, can comprise 5-10% of the mixture. The innovative algae-derived components, which significantly enhance CO2 sequestration capabilities, can make up 5-15% of the composition. This range allows for optimization of the algae-based materials' contribution to carbon capture. Carbonation accelerators can be included at 1-5% to enhance CO2 uptake during curing, while water content can be maintained between 4-6% to ensure proper workability and hydration.\|[0153] These ranges have been determined through extensive experimentation and observation by the inventor. They allow for the concrete composition in accordance with such embodiment to sequester at least 400 kg of CO2 per 1,000 kg of concrete produced, achieving a net negative carbon footprint of at least 300 kg CO2 per 1,000 kg of concrete. This flexibility in composition enables the concrete to be tailored for specific applications while maintaining its superior carbon sequestration capabilities and economic viability through tax incentives.\|[0154] The innovative features incorporated in the preferred embodiment address the limitations of previous approaches and provide a concrete composition with superior carbon sequestration capabilities. The use of brown algae-derived alginate beads, their synergistic interactions with other concrete components, and the enhanced moisture retention properties all contribute to a more effective and long-lasting carbon capture solution. This advanced concrete formulation not only reduces the carbon footprint associated with concrete production but also actively removes CO2 from the atmosphere throughout its service life, representing a significant step forward in sustainable construction materials.\|[0155] While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. It is not intended that the invention be limited by the specific examples provided within the specification. While the invention has been described with reference to the aforementioned specification, the descriptions and illustrations of the embodiments herein are not meant to be construed in a limiting sense. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. Furthermore, it shall be understood that all aspects of the invention are not limited to the specific depictions, configurations or relative proportions set forth herein which depend upon a variety of conditions and variables. It should be understood that various alternatives to the embodiments of the invention described herein may be employed in practicing the invention. It is therefore contemplated that the invention shall also cover any such alternatives, modifications, variations or equivalents. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby.	(US20250250199)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] This application claims the benefit of and incorporates by reference in its entirety U.S. Provisional Patent Application No. 63/469,108, filed May 26, 2023 which is incorporated herein by reference in its entirety. This application also claims the benefit of, is a continuation-in-part of, and incorporates by reference in its entirety U.S. patent application Ser. No. 18/722,678, filed on Jun. 21, 2024, and U.S. patent application Ser. No. 18/814,312 filed on Aug. 23, 2024. This application also claims the benefit of and incorporates by reference in its entirety International Patent Application No. PCT/US24/13913, filed Feb. 1, 2024.\|(US20250250199)\|FIELD OF THE INVENTION\|[0002] The present invention relates to the field of sustainable construction materials, specifically to carbon-sequestering concrete compositions and methods for their production.\|BACKGROUND OF THE INVENTION\|[0003] Concrete is one of the most widely used construction materials globally, with over 4 billion metric tons produced annually.\|[0004] However, conventional Portland cement concrete production is a significant contributor to global carbon dioxide emissions, accounting for 7-8% of all CO2 emissions worldwide. This represents an immense environmental burden, generating over 2 gigatons of carbon dioxide per year during cement production alone.\|[0005] Recent efforts to mitigate the carbon footprint of concrete have explored various approaches, including the incorporation of seawater and algae into concrete mixes to enable CO2 sequestration.\|[0006] However, these existing methods have achieved only modest and inconsistent levels of CO2 absorption that pale in comparison to the scale of emissions from concrete production.\|[0007] One such approach is described in Korean Patent No. 102079643 B1 to Lee et al. (“LEE”), which discloses a carbon dioxide-absorbing marine concrete composition made by mixing blast furnace slag, fly ash, metakaolin, sodium silicate, and dried algae powder. While this composition attempts to address the environmental impact of concrete production, it suffers from several significant limitations.\|[0008] The use of algae powder alone in the manner disclosed by LEE fails to fully leverage the carbon sequestration potential of marine algae, as it does not provide optimal surface area for CO2 absorption or create the necessary conditions for long-term carbon mineralization. Furthermore, simply mixing algae powder into concrete does not facilitate the formation of a matrix across the concrete surface that could enhance long-term sequestration and improve durability. There is a need for an innovative approach that can dramatically increase the CO2 absorption capacity of concrete, create synergistic interactions with other concrete components, and provide a mechanism for moisture retention to facilitate greater direct air capture of CO2. Such an approach would overcome the limitations of current algae-based concrete technologies and offer superior CO2 sequestration capabilities, enhanced durability, and improved overall performance.\|[0009] The need for carbon-capturing concrete has become increasingly urgent as the construction industry seeks to reduce its significant carbon footprint. To incentivize the adoption of such environmentally beneficial technologies, various tax credits and incentives have been established. Section 45Q of the Internal Revenue Code provides tax credits for carbon oxide sequestration, which can result in substantial savings for concrete producers utilizing this technology. Additionally, the Investment Tax Credit offers up to 30% credit on capital investments in carbon-capturing technologies. Other applicable incentives include R&D tax credits, Production Tax Credits, and various federal and state tax incentives designed to promote sustainable construction practices. These financial incentives not only make the adoption of carbon-sequestering concrete more economically viable but also align with broader policy goals of reducing greenhouse gas emissions and promoting sustainable development in the construction industry.\|[0010] These limitations result in a concrete composition that, while attempting to address environmental concerns, falls short of achieving significant and long-lasting carbon sequestration. The present invention seeks to overcome these limitations by providing a novel carbon-absorbing concrete composition and method of production that offers superior CO2 sequestration capabilities, enhanced durability, and improved overall performance compared to existing technologies.\|SUMMARY OF THE INVENTION\|[0011] The present invention relates to a carbon-sequestering concrete composition and method of production that addresses the limitations of previous approaches to reducing the carbon footprint of concrete.\|[0012] At the core of the preferred embodiment is the utilization of brown algae species, particularly “Macrocystis pyrifera”, which are transformed into alginate beads through a process called ionic gelation. These alginate beads dramatically increase the surface area available for CO2 absorption, forming a matrix across the concrete surface that enhances long-term sequestration and improves durability.\|[0013] The alginate beads are created through ionic gelation using brown algae powder. This process involves mixing the algae powder with water to create an alginate solution, which is then introduced dropwise into a bath containing calcium ions. As the droplets come into contact with the calcium ions, they undergo rapid gelation, forming stable, three-dimensional network structures with a high surface area, ideal for CO2 absorption and moisture retention in concrete.\|[0014] The preferred embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0015] The alginate beads play a crucial role in moisture retention in the context of the preferred embodiment, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0016] The preferred embodiment also addresses the formation of bicarbonate (HCO3-) ions in the presence of moisture from alginate beads, which is crucial for the carbon sequestration mechanism of the concrete. This process contributes to the concrete's ability to sequester CO2 not only during the initial curing phase but also throughout its service life.\|[0017] Furthermore, the alginate beads contribute to the self-healing of micro-cracks in the concrete, extending its lifespan and durability. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0018] In summary, the preferred embodiment provides a concrete composition with superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. It addresses the limitations of previous approaches and represents a significant advancement in sustainable construction materials.\|(US20250250199)\|BRIEF DESCRIPTION OF THE FIGURES\|[0019] FIG. 1 depicts the usage of an embodiment of the invention in association with a sidewalk.\|[0020] FIG. 2 depicts the usage of an embodiment of the invention in association with a pillar associated with a typical construction project.\|(US20250250199)\|DETAILED DESCRIPTION\|[0021] The preferred embodiment comprises a carbon-sequestering concrete and the associated methods of manufacture, addressing the limitations of previous methods and significantly enhancing CO2 absorption capabilities.\|[0022] At the core of this embodiment is the utilization of brown algae species, particularly “Macrocystis pyrifera”, which are transformed into alginate beads through a process called ionic gelation. These alginate beads dramatically increase the surface area available for CO2 absorption, forming a matrix across the concrete surface that enhances long-term sequestration and improves durability. The alginate beads in the preferred embodiment are created through a process called ionic gelation using brown algae powder, particularly from species “Macrocystis pyrifera”. This process is critical for enhancing CO2 absorption in the concrete mixture.\|[0023] The brown algae species “Macrocystis pyrifera” was chosen for creating alginate beads in the preferred embodiment due to its superior carbon sequestration capabilities. This species has evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions, making it significantly more effective for CO2 absorption compared to red and green algae species. The alginate extracted from Macrocystis pyrifera is particularly rich in carboxyl groups, which are crucial for the ionic gelation process used to form the beads. When mixed with water and introduced dropwise into a calcium ion bath, the alginate from Macrocystis pyrifera forms stable, three-dimensional network structures with a high surface area, ideal for CO2 absorption and moisture retention in concrete. In alternative embodiments, other brown algae species may serve as a substitute, including but not limited to Laminaria, Ascophyllum, Sargassum, and Fucus species. These alternative species also possess similar cell wall structures and carbon-binding capabilities, although Macrocystis pyrifera remains the preferred choice due to its particularly high alginate content and optimal gelation properties for concrete applications.\|[0024] To form the alginate beads, the brown algae powder is first mixed with water to create an alginate solution. This solution contains the alginate polymers naturally present in the cell walls of brown algae, which are rich in carboxyl groups.\|[0025] The alginate solution in an embodiment is then introduced dropwise into a bath containing divalent cations, typically calcium ions. As the alginate droplets come into contact with the calcium ions, they undergo a rapid gelation process. The calcium ions crosslink the alginate polymers, forming a stable, three-dimensional network structure. This ionic gelation process results in the formation of spherical alginate beads with a significantly increased surface area compared to the original algae powder. The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture. The ionic gelation process for forming alginate beads in an embodiment begins with mixing brown algae powder, particularly from species like “Macrocystis pyrifera”, with water to create an alginate solution. This solution contains the alginate polymers naturally present in the cell walls of brown algae, which are rich in carboxyl groups. The alginate solution is then introduced dropwise into a bath containing divalent cations, typically calcium ions. As the alginate droplets come into contact with the calcium ions, they undergo a rapid gelation process. The calcium ions crosslink the alginate polymers, forming a stable, three-dimensional network structure. This process results in the formation of spherical alginate beads with a significantly increased surface area compared to the original algae powder. The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture. The size and density of the alginate beads can be controlled by adjusting various parameters during the gelation process, such as the concentration of the alginate solution, the type and concentration of the crosslinking ions, and the droplet size. This allows for optimization of the beads' properties to suit the specific requirements of the concrete mixture. Once formed, the alginate beads are collected and may undergo further processing, such as washing to remove excess ions and drying to a desired moisture content. The resulting beads are then ready to be incorporated into the concrete mixture, where they will play a crucial role in enhancing CO2 sequestration and improving the overall performance of the concrete in accordance with an embodiment of the invention.\|[0026] The size and density of the alginate beads can be controlled by adjusting various parameters during the gelation process, such as the concentration of the alginate solution, the type and concentration of the crosslinking ions, and the droplet size. This allows for optimization of the beads' properties to suit the specific requirements of the concrete mixture.\|[0027] Once formed, the alginate beads are collected and may undergo further processing, such as washing to remove excess ions and drying to a desired moisture content. The resulting beads are then ready to be incorporated into the concrete mixture, where they will play a crucial role in enhancing CO2 sequestration and improving the overall performance of the concrete.\|[0028] The formation of these alginate beads through ionic gelation is a key innovation that sets the preferred embodiment of the invention apart from previous approaches that simply mixed algae powder into concrete. The beads provide a matrix across the surface of the concrete, dramatically enhancing long-term sequestration and improving the concrete's durability.\|[0029] The alginate beads formed from brown algae powder significantly increase the CO2 absorption surface area compared to simply using algae powder in concrete. This enhancement in surface area is achieved through the ionic gelation process, which creates a porous, three-dimensional structure within each bead.\|[0030] When algae powder is directly mixed into concrete in accordance with the preferred embodiment, it remains as discrete particles with limited surface area exposed for CO2 interaction. In contrast, the alginate beads form a matrix across the surface of the concrete, dramatically increasing the total surface area available for carbon dioxide absorption.\|[0031] The ionic gelation process creates a network of interconnected pores within each alginate bead. This porous structure allows CO2 molecules to penetrate deep into the bead, rather than just interacting with the outer surface. As a result, the effective surface area for CO2 absorption is multiplied many times over compared to solid algae powder particles in accordance with the preferred embodiment.\|[0032] Furthermore, the alginate beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. This moisture retention further enhances CO2 absorption, as the carbonation process reacts more readily in the presence of water. The combination of increased surface area and moisture retention allows for significantly more efficient CO2 capture and conversion to stable carbonate compounds.\|[0033] The size and density of the alginate beads can be controlled during the gelation process in accordance with various embodiments, allowing for optimization of the surface area to volume ratio. By adjusting parameters such as alginate concentration, crosslinking ion type and concentration, and droplet size, the beads can be tailored to maximize their CO2 absorption capacity.\|[0034] Additionally, the alginate beads create a more uniform distribution of CO2 absorption sites throughout the concrete matrix compared to algae powder. This even distribution ensures that the carbon sequestration potential is maximized across the entire concrete structure, rather than being limited to localized areas where algae powder particles might cluster.\|[0035] The cumulative effect of these factors in accordance with the preferred embodiment-increased surface area, porous structure, moisture retention, and uniform distribution-results in CO2 absorption capabilities that are orders of magnitude greater than what can be achieved with simple algae powder incorporation associated with other attempts. This dramatic enhancement in carbon sequestration efficiency is a critical innovation of the preferred embodiment of the invention, enabling concrete structures to serve as highly effective carbon sinks throughout their service life.\|[0036] The preferred embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS).\|[0037] These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption. The alginate beads also play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2.\|[0038] The preferred embodiment enhances pozzolanic reactions through the synergistic interaction between alginate beads and various components of the concrete mix, particularly fly ash and metakaolin.\|[0039] Pozzolanic reactions occur when siliceous or aluminosiliceous materials react with calcium hydroxide in the presence of water to form compounds with cementitious properties. In the context of this invention, the alginate beads create localized high-humidity environments within the concrete matrix, which facilitates these reactions. The increased moisture content provided by the beads promotes the dissolution of silica and alumina from the pozzolanic materials, allowing them to react more readily with calcium hydroxide produced during the hydration of cement or geopolymer precursors. This enhanced reactivity leads to the formation of additional calcium silicate hydrate (C—S—H) and calcium aluminate hydrate (C-A-H) gels, which contribute to the concrete's strength and durability. Furthermore, the pozzolanic reactions consume calcium hydroxide, reducing the concrete's susceptibility to chemical attacks and improving its long-term performance. The increased pozzolanic activity also creates more sites for carbon dioxide capture within the concrete composition, as the newly formed C—S—H and C-A-H gels provide additional surface area for CO2 absorption and carbonation.\|[0040] The preferred embodiment creates additional sites for carbon dioxide capture through several mechanisms. The alginate beads formed from brown algae powder increase the surface area available for CO2 absorption, creating a matrix across the concrete surface that enhances long-term sequestration. This matrix structure provides numerous additional sites for CO2 to interact with and be captured by the concrete. Furthermore, the synergistic interactions between the alginate beads and other concrete components, such as fly ash and ground granulated blast furnace slag (GGBFS), lead to enhanced pozzolanic reactions in association with the preferred embodiment.\|[0041] These reactions create more sites in the concrete composition specifically for capturing carbon dioxide. The increased pozzolanic activity results in the formation of additional calcium silicate hydrate (C—S—H) and calcium aluminate hydrate (C-A-H) gels, which provide extra surface area for CO2 absorption and carbonation. The alginate beads also interact positively with other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4).\|[0042] The alginate beads in the preferred embodiment interact synergistically with additives like magnesium carbonate and olivine (Mg2SiO4) to enhance the concrete's CO2 sequestration capabilities. The moisture retention properties of the alginate beads play a crucial role in facilitating these interactions.\|[0043] For magnesium carbonate, the localized high-humidity environments created by the alginate beads promote its gradual dissolution within the concrete matrix. This dissolution process releases magnesium ions, which can then react with dissolved CO2 to form stable magnesium carbonate compounds, effectively capturing and storing atmospheric carbon dioxide.\|[0044] In the case of olivine (Mg2SiO4), the humidity retained by the alginate beads creates conditions favorable for its dissolution in accordance with the preferred embodiment. As the olivine dissolves, it releases magnesium ions into the concrete matrix. These magnesium ions can then interact with the alginate structure, enhancing the formation of magnesium carbonates. This process not only contributes to additional CO2 sequestration but also improves the overall strength and durability of the concrete.\|[0045] The alginate beads create “localized high-humidity environments” within the concrete through their unique moisture absorption and retention properties. When incorporated into the concrete mixture, these beads absorb and hold water, acting as microscopic reservoirs distributed throughout the concrete matrix.\|[0046] In accordance with the preferred embodiment, as the concrete cures and ages, the alginate beads continue to retain this moisture, creating small pockets of high humidity surrounding each bead. These localized high-humidity environments are crucial for facilitating CO2 absorption, as the carbonation process reacts more readily in the presence of water. The retained moisture provides a medium for atmospheric CO2 to dissolve, forming carbonic acid which then interacts with calcium ions to produce stable calcium carbonate. This process of CO2 absorption and carbonate formation is significantly enhanced by the consistent availability of moisture provided by the alginate beads, allowing for continuous carbon sequestration throughout the concrete's service life. Furthermore, these high-humidity microenvironments promote the gradual dissolution of other additives like magnesium carbonate and olivine, further enhancing the concrete's overall CO2 absorption capacity.\|[0047] The continuous moisture provision by the alginate beads ensures that these reactions can occur over an extended period, prolonging the concrete's carbon capture capabilities. As atmospheric CO2 dissolves in the water retained by the beads, it forms carbonic acid, which then reacts with the magnesium ions released from both magnesium carbonate and olivine to produce stable carbonate compounds. These interactions between the alginate beads and additives like magnesium carbonate and olivine create a self-sustaining cycle of CO2 absorption and mineralization within the concrete. The process continues throughout the concrete's service life, significantly enhancing its long-term carbon sequestration potential compared to traditional concrete compositions.\|[0048] The preferred embodiment prolongs the period of CO2 absorption through several innovative mechanisms. The alginate beads formed from brown algae powder play a crucial role in extending the carbon sequestration capabilities of the concrete over time. These beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix that facilitate ongoing CO2 absorption.\|[0049] The synergistic interactions between the alginate beads and other concrete components, such as ground granulated blast furnace slag (GGBFS), increase both the hydration and carbonation processes. This effectively extends the duration during which the concrete can actively absorb carbon dioxide from the atmosphere.\|[0050] Furthermore, the alginate beads enhance the CO2 sequestration capabilities of other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4). The humidity retained by the beads creates conditions that promote the gradual dissolution of these minerals, leading to sustained carbon capture over an extended period. The continuous process of CO2 absorption is supported by the ongoing formation of carbonate compounds within the concrete matrix.\|[0051] The alginate beads facilitate the dissolution of minerals including olivine (Mg2SiO4) to enhance carbon capture through several mechanisms. The beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. This increased moisture content promotes the gradual dissolution of olivine, releasing magnesium ions into the surrounding concrete. The humidity in the alginate beads creates these localized high moisture environments, which are crucial for facilitating olivine dissolution. As the olivine dissolves, the released magnesium ions interact with the alginate structure, enhancing the formation of magnesium carbonates. This process not only contributes to additional CO2 sequestration but also improves the overall strength and durability of the concrete. The continuous moisture provision by the alginate beads ensures that these reactions can occur over an extended period, prolonging the concrete's carbon capture capabilities. Furthermore, the beads provide additional surface area for basalt dissolution, which leads to further carbon capture. This synergistic interaction between the alginate beads and olivine creates a self-sustaining cycle of CO2 absorption and mineralization within the concrete, significantly enhancing its long-term carbon sequestration potential compared to traditional concrete compositions.\|[0052] As atmospheric CO2 dissolves in the water retained by the alginate beads, it forms carbonic acid, which then reacts with calcium ions to produce stable calcium carbonate. This cycle of absorption and mineralization continues throughout the concrete's service life, significantly prolonging its CO2 sequestration capabilities.\|[0053] Additionally, the formation of stable calcium carbonate contributes to the self-healing of micro-cracks in the concrete. This self-healing property not only extends the overall lifespan of the concrete but also maintains its ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure. The alginate beads also contribute to the self-healing of micro-cracks in the concrete through several mechanisms. As the concrete cures and ages, the alginate beads continue to absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. When micro-cracks form, these moist environments facilitate the ongoing formation of carbonate compounds. As atmospheric CO2 dissolves in the water retained by the alginate beads, it forms carbonic acid, which then reacts with calcium ions to produce stable calcium carbonate. This calcium carbonate precipitates within the micro-cracks, gradually filling them and restoring the concrete's integrity. The continuous nature of this process, enabled by the moisture-retaining properties of the alginate beads, allows for ongoing self-healing throughout the concrete's service life. Additionally, the alginate beads' ability to enhance pozzolanic reactions and create additional sites for carbon dioxide capture contributes to the formation of supplementary binding materials that can further aid in crack repair. This self-healing property not only extends the overall lifespan of the concrete but also maintains its ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0054] By incorporating these innovative features, the preferred embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0055] The humidity retained by the alginate beads creates localized high moisture environments that facilitate the dissolution of these minerals, leading to further carbon capture opportunities. This process increases the overall number of sites available for CO2 sequestration within the concrete matrix. Lastly, the moisture retention properties of the alginate beads create conditions favorable for the ongoing formation of carbonate compounds throughout the concrete.\|[0056] As CO2 dissolves in the water absorbed by the beads, it forms carbonic acid, which then interacts with calcium ions to form stable calcium carbonate. This continuous process effectively creates new sites for carbon dioxide capture as the concrete ages, prolonging its CO2 sequestration capabilities over time.\|[0057] This innovative concrete composition not only reduces the carbon footprint associated with production but also actively removes CO2 from the atmosphere throughout its service life. The carbon capture process in the preferred embodiment occurs strongly over the initial approximately 60 days due to the rapid initial reactions between the alginate beads and atmospheric CO2, but continues on a smaller scale for many years thereafter.\|[0058] This prolonged sequestration is enabled by several key mechanisms:\|[0059] During the initial curing period, the alginate beads formed through ionic gelation provide a large surface area for CO2 absorption, allowing for rapid carbonation reactions. The beads absorb and retain moisture, creating localized high-humidity environments that facilitate the dissolution of CO2 and its reaction with calcium ions to form stable calcium carbonate.\|[0060] As the concrete continues to age, the synergistic interactions between the alginate beads and other components of the mix, such as ground granulated blast furnace slag (GGBFS) and fly ash, sustain the carbon capture process. These interactions lead to ongoing pozzolanic reactions and the creation of additional sites for CO2 absorption, albeit at a slower rate than during the initial curing period.\|[0061] The moisture retention properties of the alginate beads play a crucial role in maintaining conditions favorable for long-term CO2 sequestration. Even as the concrete ages, the beads continue to absorb and retain water from the environment, providing a medium for CO2 to dissolve and react with available calcium ions.\|[0062] Furthermore, the formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete. This self-healing process not only extends the lifespan of the concrete but also maintains pathways for continued CO2 absorption over many years.\|[0063] The gradual dissolution of minerals such as magnesium carbonate and olivine, facilitated by the moisture retained in the alginate beads, provides a slow but steady source of reactive components for ongoing CO2 sequestration. This process continues at a reduced rate long after the initial curing period, allowing the concrete to capture carbon dioxide from the atmosphere throughout its service life.\|[0064] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions in the alginate beads contributes to the self-healing of micro-cracks, further extending the concrete's lifespan and durability. By addressing the limitations of previous approaches, this invention represents a significant advancement in sustainable construction materials, offering superior carbon sequestration capabilities, enhanced durability, and improved overall performance.\|[0065] The preferred embodiment of the present invention addresses the limitations of previous approaches by utilizing brown algae species, particularly “Macrocystis pyrifera”, which have evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions. This makes them significantly more effective for CO2 absorption compared to red and green algae species. The use of brown algae provides a more efficient and targeted approach to carbon sequestration in concrete, leveraging their natural adaptations to marine environments.\|[0066] A critical innovation in the preferred embodiment is the formation of alginate beads using brown algae powder through a process called ionic gelation. This process dramatically increases the surface area available for CO2 absorption, enhancing it by orders of magnitude compared to simply mixing algae powder into the concrete. The alginate beads form a matrix across the surface of the concrete, which significantly enhances long-term sequestration and improves the concrete's durability. This matrix structure allows for more uniform and efficient carbon dioxide capture throughout the concrete, leading to superior performance over extended periods.\|[0067] The formation of alginate beads offers several key advantages over traditional methods. The increased surface area provided by the beads allows for more efficient CO2 absorption, while also promoting the formation of more stable calcium carbonate. This stability is crucial for long-term carbon sequestration, ensuring that the captured CO2 remains locked within the concrete structure for extended periods. Additionally, the uniform distribution of alginate beads throughout the concrete mix ensures that the CO2 capture potential is evenly spread, maximizing the overall sequestration capacity of the concrete.\|[0068] The alginate beads in the preferred embodiment interact synergistically with other components of the concrete mix, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance the overall performance and carbon sequestration capabilities of the concrete. For instance, the presence of alginate beads leads to enhanced pozzolanic reactions with fly ash, creating more sites within the concrete composition for capturing carbon dioxide. This increased reactivity not only improves the concrete's strength but also its ability to absorb CO2 over time.\|[0069] In the case of GGBFS, the alginate beads increase both the hydration and carbonation processes, effectively prolonging the period during which the concrete can absorb carbon dioxide. This extended absorption window is crucial for maximizing the total amount of CO2 sequestered over the lifetime of the concrete structure. Similarly, the interaction between alginate beads and metakaolin results in increased pozzolanic activity, further enhancing the concrete's performance and carbon capture capabilities.\|[0070] The alginate beads also enhance the CO2 sequestration capabilities of other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4). The beads create localized high-moisture environments that facilitate the dissolution of these minerals, leading to increased formation of carbonate compounds. This synergistic effect amplifies the overall carbon sequestration potential of the concrete, making it significantly more effective at reducing atmospheric CO2 levels compared to traditional concrete formulations.\|[0071] One of the most crucial roles played by the alginate beads in the preferred embodiment is in moisture retention, which is essential for the carbon sequestration process. The beads absorb and retain water, creating localized high-humidity environments within the concrete matrix. This increased moisture content is vital for facilitating greater direct air capture (DAC) of CO2, as the carbonation process reacts more readily in the presence of water. The absorbed water acts as a medium in which CO2 can dissolve, forming carbonic acid (H2CO3) and initiating a series of chemical reactions that lead to carbon sequestration.\|[0072] The presence of moisture within the alginate beads creates conditions favorable for the formation of bicarbonate (HCO3-) ions. This process is fundamental to the sequestration of various compounds within the concrete matrix. As CO2 dissolves and forms carbonic acid, it interacts with the calcium ions present within the alginate beads. This interaction leads to the formation of stable calcium carbonate, effectively locking the captured CO2 into the concrete structure. This process not only increases the overall CO2 uptake but also contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability.\|[0073] The formation of bicarbonate (HCO3-) ions in the presence of moisture from alginate beads is a crucial process in the carbon sequestration mechanism of the concrete. The alginate beads, which are rich in carboxyl groups, absorb and retain water, creating localized high-humidity environments within the concrete matrix. As atmospheric CO2 dissolves in this water, it forms carbonic acid (H2CO3). In the presence of moisture, the carboxyl groups in the alginate react with this carbonic acid, leading to the formation of bicarbonate (HCO3-) ions.\|[0074] This process is critical in accordance with the preferred embodiment because the bicarbonate ions serve as an intermediate step in the overall carbon mineralization process. The bicarbonate ions can further react with calcium ions within the alginate beads or from other sources in the concrete to form stable calcium carbonate (CaCO3). This reaction sequence effectively locks in the absorbed CO2, converting it from a gaseous form to a solid, stable mineral form within the concrete structure. The continuous moisture provision by the alginate beads ensures that this bicarbonate formation process can occur over an extended period, prolonging the concrete's carbon capture capabilities. This ongoing process contributes to the concrete's ability to sequester CO2 not only during the initial curing phase but also throughout its service life, albeit at a slower rate in later stages.\|[0075] An embodiment of the present invention comprises a carbon-sequestering concrete composition with specific components and their respective percentages by mass. Alternative embodiments deviate slightly from the specific percentages by mass presented in the foregoing.\|[0076] The composition includes Fly Ash (Class F) at 25%, which serves as the primary binder and significantly reduces CO2 emissions compared to traditional cement. This component allows for increased CO2-reactive materials in the mixture, enhancing the overall carbon sequestration potential of the concrete.\|[0077] Ground Granulated Blast Furnace Slag (GGBFS) constitutes 20% of the mixture. This component enhances the strength and durability of the concrete while acting as a supplementary binder. The inclusion of GGBFS contributes to the reduction of the carbon footprint associated with concrete production by partially replacing traditional cement.\|[0078] Metakaolin, comprising 5% of the mixture, improves early strength and reduces permeability of the concrete. This component allows room for more CO2 capture materials, further enhancing the carbon sequestration capabilities of the concrete. The inclusion of metakaolin also contributes to the overall sustainability of the mixture by reducing the need for energy-intensive cement production.\|[0079] Recycled Aggregates make up 20% of the composition, while Natural Aggregates constitute 15%. The use of recycled aggregates significantly reduces the environmental impact of the concrete production process by minimizing the need for new raw materials extraction. Natural aggregates provide the necessary mechanical strength to the concrete. The balance between recycled and natural aggregates is carefully optimized to maintain the structural integrity of the concrete while maximizing its sustainability.\|[0080] Silica Fume, at 2% of the mixture, fills micro-pores and enhances the strength and durability of the concrete. This component improves the overall pore structure of the concrete, which is crucial for both strength development and carbon sequestration potential. The fine particles of silica fume react with calcium hydroxide produced during cement hydration, forming additional calcium silicate hydrate (C—S—H) gel, which enhances the concrete's properties.\|[0081] Sodium Hydroxide (NaOH) and Sodium Silicate (Na2SiO3) serve as activators for the geopolymerization process, constituting 1.5% and 2.5% of the mixture respectively. These components are essential for activating the aluminosilicate materials in the mixture, particularly the fly ash and GGBFS. The careful balance of these activators ensures optimal reaction efficiency while minimizing environmental impact.\|[0082] Algae Biomass, used for creating alginate beads, makes up 2% of the mixture. This component is crucial for maximizing CO2 sequestration potential through the formation of alginate beads and direct air capture. The algae biomass is transformed into alginate beads through a process called ionic gelation, which dramatically increases the surface area available for CO2 absorption.\|[0083] Calcium Carbonate (CaCO3) and Magnesium Carbonate (MgCO3) each constitute 2% of the mixture. These components enhance carbonation during curing and beyond, improving overall CO2 capture. They react with CO2 to form stable carbonate compounds, effectively sequestering carbon within the concrete structure.\|[0084] Silica from Algae, comprising 1% of the mixture, serves as a sustainable silica source that improves strength with minimal environmental impact. This component contributes to the overall sustainability of the concrete mixture while enhancing its mechanical properties.\|[0085] Magnesium Silicate and Olivine (finely ground) each make up 1% of the mixture. These components enhance CO2 sequestration through mineral carbonation. The fine grinding of olivine increases its surface area, making it more reactive and efficient in capturing CO2. These materials react with atmospheric CO2 to form stable carbonate minerals, effectively locking away carbon for long periods.\|[0086] Basalt Rock Dust, constituting 1% of the mixture, provides trace minerals and enhances CO2 uptake through mineral carbonation. This component contributes to the overall carbon sequestration potential of the concrete while also improving its mechanical properties.\|[0087] Biochar (Activated) makes up 1% of the mixture. This component sequesters carbon and improves internal curing of the concrete. Biochar's porous structure allows it to absorb and retain CO2, contributing significantly to the overall carbon sequestration capabilities of the concrete.\|[0088] Alginate Beads, maximized at 1.5% of the mixture, play a crucial role in enhancing CO2 capture. These beads, formed through ionic gelation of brown algae powder, dramatically increase the surface area available for CO2 absorption. They form a matrix across the concrete surface, significantly enhancing long-term sequestration and improving durability.\|[0089] Carbonation Accelerators (C—S—H Seeds) constitute 1.5% of the mixture. These accelerate strength gain and CO2 uptake during curing. The C—S—H seeds provide nucleation sites for the formation of additional calcium silicate hydrate gel, which not only enhances the concrete's strength but also increases its capacity to absorb CO2.\|[0090] Water, making up 1% of the mixture, is necessary for workability and chemical reactions. The water content is carefully controlled to ensure optimal hydration of cementitious materials and proper workability of the concrete mix, while also facilitating the various chemical reactions involved in CO2 sequestration.\|[0091] This embodiment of the carbon-sequestering concrete composition demonstrates superior carbon sequestration capabilities compared to conventional concrete. For every 1,000 tons of concrete produced, this embodiment emits 81.4 tons of CO2 but sequesters 91.25 tons of CO2, resulting in a net sequestration of 9.85 tons of CO2. This represents a total reduction of 909.85 tons of CO2 per 1,000 tons produced, or a 101.1% reduction compared to conventional concrete.\|[0092] The CO2 sequestration in this embodiment occurs through several mechanisms, including biochar absorption, algae biomass uptake, carbonates reaction, mineral carbonation, alginate bead absorption, and CO2 absorption during curing. The total CO2 sequestered amounts to 91,250 kg (91.25 tonnes) per 1,000 tons of concrete produced.\|[0093] The carbon-sequestering concrete composition described in this embodiment demonstrates remarkable carbon sequestration capabilities that significantly outperform conventional concrete. For every 1,000 tons of concrete produced, this innovative composition achieves a net carbon sequestration of 9.85 tons of CO2, in stark contrast to conventional concrete which emits approximately 900 tons of CO2 for the same amount produced. This results in a total reduction of 909.85 tons of CO2 per 1,000 tons produced, representing a 101.1% reduction compared to conventional concrete.\|[0094] The superior carbon sequestration performance of this concrete composition is achieved through a combination of reduced emissions during production and active carbon capture mechanisms. While the embodiment emits 81.4 tons of CO2 during production, it sequesters 91.25 tons of CO2, resulting in the net negative carbon footprint. This remarkable feat is accomplished through several key mechanisms that work synergistically to capture and store carbon dioxide.\|[0095] The CO2 sequestration in this embodiment occurs through several primary mechanisms, including the following: Biochar absorption, which accounts for 29,333 kg of CO2 sequestered. The activated biochar in the mixture acts as a highly effective carbon sink due to its porous structure and high surface area. Algae Biomass uptake, responsible for sequestering 36,667 kg of CO2. The algae biomass, particularly when transformed into alginate beads, provides a substantial contribution to the overall carbon capture capacity of the concrete. Carbonates Reaction, which sequesters 2,000 kg of CO2. This involves the reaction of CO2 with calcium and magnesium carbonates present in the mixture, forming stable carbonate compounds. Mineral Carbonation, accounting for 2,500 kg of CO2 sequestered. This process involves the reaction of CO2 with minerals such as magnesium silicate and olivine to form stable carbonate minerals. Alginate Beads, which directly capture 750 kg of CO2 but also play a crucial role in enhancing the capture efficiency of other materials. The alginate beads, formed through ionic gelation of brown algae powder, create a matrix across the concrete surface that significantly increases the surface area available for CO2 absorption. CO2 absorbed during curing, which accounts for 20,000 kg of the total CO2 sequestered. This substantial amount is captured during the initial setting and hardening phase of the concrete.\|[0096] These mechanisms in an embodiment collectively result in a total CO2 sequestration of 91,250 kg (91.25 tonnes) per 1,000 tons of concrete produced. The synergistic interactions between the various components, particularly the alginate beads and other concrete constituents like geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS), enhance pozzolanic reactions and create additional sites for carbon dioxide capture. Furthermore, the moisture retention properties of the alginate beads create localized high-humidity environments within the concrete, facilitating greater direct air capture of CO2 throughout the concrete's service life.\|[0097] This innovative concrete composition not only addresses the carbon emissions associated with concrete production but also actively removes CO2 from the atmosphere, representing a significant advancement in sustainable construction materials.\|[0098] This embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0099] The alginate beads, formed through ionic gelation of brown algae powder, play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0100] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0101] By incorporating these innovative features, this embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0102] An alternative embodiment of the present invention comprises a carbon-sequestering concrete composition with the following components and their respective percentages by mass\| - Fly Ash (Class F): 22%\| - Ground Granulated Blast Furnace Slag (GGBFS): 20%\| - Metakaolin: 4%\| - Recycled Aggregates: 20%\| - Natural Aggregates: 12%\| - Silica Fume: 3%\| - Sodium Hydroxide (NaOH): 1%\| - Sodium Silicate (Na2SiO3): 2%\| - Algae Biomass (for Beads): 3%\| - Calcium Carbonate (CaCO3): 3%\| - Magnesium Carbonate (MgCO3): 3%\| - Silica from Algae: 1%\| - Magnesium Silicate: 2%\| - Olivine (Finely Ground): 3%\| - Basalt Rock Dust: 2%\| - Biochar (Activated): 2%\| - Alginate Beads (Maximized): 3%\| - Carbonation Accelerators (C—S—H Seeds): 2%\| - Water: 1%\|[0122] In this alternative embodiment, the Fly Ash (Class F) content is reduced to 22% in such embodiment to allow for increased CO2-reactive materials. This adjustment maintains the primary binding function while enhancing the overall carbon sequestration potential of the concrete. The Ground Granulated Blast Furnace Slag (GGBFS) in such embodiment is included at 20%, continuing to enhance strength and durability while acting as a supplementary binder. This component contributes significantly to reducing the carbon footprint associated with concrete production. Metakaolin is reduced to 4% in such embodiment, still improving early strength and reducing permeability while allowing for more CO2 capture materials. This adjustment contributes to the overall sustainability of the mixture. The ratio of Recycled Aggregates to Natural Aggregates is adjusted to 20% and 12% respectively in accordance with such embodiment. This change further reduces the environmental impact of the concrete production process while maintaining necessary mechanical strength. Silica Fume is increased to 3% to enhance the pore structure, strength, and durability of the concrete. This increase improves the overall performance and CO2 sequestration potential. The activators, Sodium Hydroxide (NaOH) and Sodium Silicate (Na2SiO3), are adjusted to 1% and 2% respectively. This optimization balances the geopolymerization process while minimizing environmental impact. Algae Biomass for beads is increased to 3%, maximizing CO2 sequestration potential through enhanced alginate bead formation and direct air capture. Both Calcium Carbonate (CaCO3) and Magnesium Carbonate (MgCO3) are increased to 3% each in accordance with this embodiment, enhancing carbonation during curing and beyond, thus improving overall CO2 capture. Magnesium Silicate is increased to 2%, and Olivine (Finely Ground) to 3%, enhancing CO2 sequestration through increased mineral carbonation potential. Basalt Rock Dust is increased to 2%, providing more trace minerals and enhancing CO2 uptake through mineral carbonation. Biochar (Activated) is increased to 2%, improving carbon sequestration and internal curing of the concrete. Alginate Beads are included at 3% in accordance with such embodiment, significantly enhancing CO2 capture and improving the concrete's overall performance. Carbonation Accelerators (C—S—H Seeds) are increased to 2%, further accelerating strength gain and CO2 uptake during curing. Water content remains at 1%, maintaining the necessary workability and facilitating chemical reactions.\|[0123] This alternative embodiment demonstrates enhanced carbon sequestration capabilities. For every 1,000 tons of concrete produced, this embodiment creates approximately 64.2 tons of CO2 but sequesters 101 tons of CO2 through direct air capture (DAC) and mineralization. This results in a net sequestration of approximately 36.8 tons of CO2 per 1,000 tons of concrete produced in accordance with an exemplary implementation.\|[0124] The carbon sequestration in this embodiment occurs through several mechanisms, including biochar absorption, algae biomass uptake, carbonates reaction, mineral carbonation, alginate bead absorption, and CO2 absorption during curing. The total CO2 sequestered amounts to 101,000 kg (101 tonnes) per 1,000 tons of concrete produced.\|[0125] This embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0126] The alginate beads, formed through ionic gelation of brown algae powder, play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0127] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability in an embodiment. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0128] By incorporating these innovative features and optimizing the component ratios, this alternative embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0129] The carbon-sequestering concrete composition described in the embodiments of the invention in an example is designed to maximize eligibility for significant tax credits and incentives, potentially resulting in substantial cost savings for concrete producers and users. In an example, the tax credits could be allocated for 1,000 tons of concrete produced as an embodiment of the invention in accordance with the following:\|[0130] Section 45Q tax credits could provide approximately $100,000 to $150,000 in savings per 1,000 tons of concrete produced, depending on the final determination by the EPA/IRS and the results of a Life Cycle Assessment (LCA). This estimate is based on the net carbon sequestration capabilities of the concrete, which ranges from 9.85 to 36.8 tons of CO2 per 1,000 tons of concrete produced, depending on the specific embodiment.\|[0131] The Investment Tax Credit could cover up to 30% of a concrete mixer's investment in this carbon-sequestering concrete technology. This credit would apply to the capital expenditures required to implement the new production methods and equipment necessary for manufacturing this innovative concrete.\|[0132] Additional tax incentives that may be applicable in association with and as an expected benefit of an embodiment of the invention include:\|[0133] R&D tax credits for the ongoing development and improvement of the carbon-sequestering concrete technology. Production Tax Credits for the manufacture of environmentally beneficial products. Various federal and state tax incentives designed to promote sustainable construction practices and materials.\|[0134] When considering a larger scale of production, for example 20 medium sized building construction projects, the total savings from these combined tax credits and incentives could exceed $5 million for a concrete producer. This estimate takes into account the cumulative effect of the various tax benefits across multiple projects.\|[0135] The economic benefits of these tax credits extend beyond mere cost savings. They also enhance the competitiveness of the carbon-sequestering concrete in the market. Before applying any tax credits, the price of this innovative concrete is approximately $138 per ton, which is already competitive with conventional concrete. However, after factoring in the tax credits, the effective price drops to around $112 per ton, making it more economical than conventional concrete options.\|[0136] In accordance with various embodiments, the exact allocation and amount of tax credits may vary depending on factors such as the specific project details, the concrete producer's financial situation, and any changes in tax laws or regulations. Additionally, the realization of these tax benefits would likely require careful documentation of the carbon sequestration capabilities of the concrete, as well as compliance with relevant regulatory requirements, which is an intended use in accordance with an embodiment of the invention.\|[0137] Another embodiment of the invention comprises a carbon-sequestering concrete composition optimized for maximum CO2 sequestration and economic viability through tax incentives, as follows:\|[0138] The composition of this carbon-sequestering concrete in such embodiment is carefully formulated to maximize both CO2 sequestration capabilities and eligibility for tax credits. The mixture, designed for a 1,000-ton batch, comprises several key components that work synergistically to achieve these goals.\|[0139] Aluminosilicate materials form the foundation of the geopolymer binder system in such embodiment. These include 30% Fly Ash (Class F), 20% Ground Granulated Blast Furnace Slag (GGBFS), 5% Metakaolin, and 3% Silica Fume. These materials not only contribute to the strength and durability of the concrete but also play a crucial role in CO2 sequestration through pozzolanic reactions.\|[0140] A significant portion of the mix in such embodiment is dedicated to CO2-absorbing materials. This includes 15% Magnesium Silicate, 15% finely ground Olivine, 10% Activated Biochar, 3% Calcium Carbonate (CaCO3), and 2% Magnesium Carbonate (MgCO3). These components are specifically chosen for their high CO2 sequestration potential and their ability to form stable carbonate compounds over time.\|[0141] The aggregate portion of the mix consists of 10% Natural Aggregates and 5% Recycled Aggregates, balancing structural requirements with sustainability considerations in accordance with such embodiment. The alkaline activators, crucial for the geopolymerization process, include 2% Sodium Hydroxide (NaOH) and 4% Sodium Silicate (Na2SiO3).\|[0142] A key innovation in this embodiment is the incorporation of algae-derived components. This comprises 1% Silica from Algae, 3% Algae Biomass for bead formation, and 5% Alginate Beads. These components significantly enhance the CO2 sequestration capabilities of the concrete through increased surface area and the creation of localized high-humidity environments that facilitate CO2 absorption.\|[0143] The mixture in such embodiment also comprises 2% Carbonation Accelerators in the form of C—S—H Seeds, which enhance the rate of CO2 uptake during the curing process. The water content is maintained at 5%, with small amounts of superplasticizers (0.5%) and air-entraining agents (0.1%) added to optimize workability and durability.\|[0144] The production process of this concrete composition in such embodiment has been observed by the inventor to result in total emissions of 108,550 kg CO2 per 1,000 tons produced. However, the CO2 sequestration capabilities of the mixture are substantial, with a total CO2 sequestration potential of 435,000 kg CO2 per 1,000 tons of concrete. This results in a net negative carbon footprint of −326,450 kg CO2 per 1,000 tons of concrete produced in accordance with inventor observations.\|[0145] The CO2 sequestration occurs through several mechanisms in accordance with such embodiment. The Magnesium Silicate and Olivine each sequester 45,000 kg CO2. The Activated Biochar contributes significantly with 200,000 kg CO2 sequestered. The Algae Biomass and Alginate Beads together sequester 80,000 kg CO2. The Calcium and Magnesium Carbonates add another 5,000 kg CO2 to the total. Additionally, the CO2 curing process is estimated to sequester an additional 50,000 kg CO2.\|[0146] This embodiment is designed to maximize eligibility for tax credits, particularly the Section 45Q tax credit for carbon oxide sequestration. For every 1,000 tons of concrete produced, this composition is eligible for approximately $26,100 in Section 45Q tax credits. When combined with other available tax credits such as the Investment Tax Credit and R&D credits, the total tax credits per 1,000 tons could reach approximately $354,100 in accordance with the regulations in place as of September 2024.\|[0147] The economic viability of this concrete composition in such embodiment is further enhanced by these tax incentives. After accounting for all applicable tax credits, the effective cost of this concrete is estimated to be $57.85 per ton, making it highly competitive in the market.\|[0148] In comparison to other carbon-reducing concrete technologies, this embodiment demonstrates superior performance. For instance, when compared to Blue Planet's concrete, which sequesters 330 tons CO2 per 1,000 tons of concrete, this embodiment sequesters 435 tons CO2. This results in higher eligibility for Section 45Q tax credits and overall tax credits under applicable regulations in place in September 2024.\|[0149] The enhanced CO2 sequestration capabilities of this concrete composition in such embodiment are achieved through the synergistic interactions between its components, particularly the alginate beads and other concrete constituents like geopolymers, fly ash, and ground granulated blast furnace slag. These interactions enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The moisture retention properties of the alginate beads create localized high-humidity environments within the concrete, facilitating greater direct air capture of CO2 throughout the concrete's service life.\|[0150] This innovative concrete composition in accordance with such embodiment not only addresses the carbon emissions associated with concrete production but also actively removes CO2 from the atmosphere, representing a significant advancement in sustainable construction materials. Its superior carbon sequestration capabilities, combined with its economic viability through tax incentives, position it as a potentially disruptive technology in the concrete industry.\|[0151] The carbon-sequestering concrete composition described in the embodiment can be formulated with varying proportions of its key components to optimize performance and CO2 sequestration capabilities. The aluminosilicate materials, which form the foundation of the geopolymer binder system, can range from 30-60% of the total composition. This range allows for flexibility in adjusting the mix based on specific project requirements and material availability. The CO2-absorbing materials, crucial for the concrete's carbon sequestration properties, can constitute 30-50% of the mixture. This range ensures a significant portion of the concrete is dedicated to active CO2 absorption while maintaining structural integrity.\|[0152] The aggregate portion, balancing structural requirements with sustainability considerations, can range from 10-20% of the total composition in accordance with such embodiment. The alkaline activators, essential for the geopolymerization process, can comprise 5-10% of the mixture. The innovative algae-derived components, which significantly enhance CO2 sequestration capabilities, can make up 5-15% of the composition. This range allows for optimization of the algae-based materials' contribution to carbon capture. Carbonation accelerators can be included at 1-5% to enhance CO2 uptake during curing, while water content can be maintained between 4-6% to ensure proper workability and hydration.\|[0153] These ranges have been determined through extensive experimentation and observation by the inventor. They allow for the concrete composition in accordance with such embodiment to sequester at least 400 kg of CO2 per 1,000 kg of concrete produced, achieving a net negative carbon footprint of at least 300 kg CO2 per 1,000 kg of concrete. This flexibility in composition enables the concrete to be tailored for specific applications while maintaining its superior carbon sequestration capabilities and economic viability through tax incentives.\|[0154] The innovative features incorporated in the preferred embodiment address the limitations of previous approaches and provide a concrete composition with superior carbon sequestration capabilities. The use of brown algae-derived alginate beads, their synergistic interactions with other concrete components, and the enhanced moisture retention properties all contribute to a more effective and long-lasting carbon capture solution. This advanced concrete formulation not only reduces the carbon footprint associated with concrete production but also actively removes CO2 from the atmosphere throughout its service life, representing a significant step forward in sustainable construction materials.\|[0155] While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. It is not intended that the invention be limited by the specific examples provided within the specification. While the invention has been described with reference to the aforementioned specification, the descriptions and illustrations of the embodiments herein are not meant to be construed in a limiting sense. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. Furthermore, it shall be understood that all aspects of the invention are not limited to the specific depictions, configurations or relative proportions set forth herein which depend upon a variety of conditions and variables. It should be understood that various alternatives to the embodiments of the invention described herein may be employed in practicing the invention. It is therefore contemplated that the invention shall also cover any such alternatives, modifications, variations or equivalents. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby.	Family Number\|(112475776)\|112475776\|Abstract\|(US20250250199 A1)\|A carbon-sequestering concrete composition and method of production are disclosed. The composition comprises geopolymer binder components, aggregates, and alginate beads formed from brown algae powder through ionic gelation. The alginate beads significantly increase CO2 absorption surface area compared to algae powder, creating a matrix across the concrete surface that enhances long-term sequestration and improves durability. The beads interact synergistically with other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag, to enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The alginate beads also facilitate the dissolution of minerals like olivine, further enhancing carbon capture. The composition demonstrates superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. The method includes forming alginate beads, incorporating them into the concrete mixture, and allowing for initial hardening and drying processes that promote carbon dioxide absorption directly from the air.\|Advantages / Prev. Drawbacks\|(US20250250199 A1)\| (...) The use of brown algae provides a more efficient and targeted approach to carbon sequestration in concrete, leveraging their natural adaptations to marine environments.\|By addressing the limitations of previous approaches, this invention represents a significant advancement in sustainable construction materials, offering superior carbon sequestration capabilities, enhanced durability, and improved overall performance.\|By incorporating these innovative features, the preferred embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|Independent Claims\|(US20250250199 A1)\| (...) at least one carbon dioxide sequestration enhancer selected from the group consisting of biochar, calcium carbonate, magnesium carbonate, magnesium silicate, olivine, and basalt rock dust.\|	Materials, metallurgy\|Other special machines	B28B-001/14\|B28B-001/54\|B28C-009/00/2\|C04B-012/00/5\|C04B-014/04/2\|C04B-014/06\|C04B-014/10/6\|C04B-014/26\|C04B-018/02/2\|C04B-018/08\|C04B-018/14/2\|C04B-022/00863\|C04B-022/10\|C04B-024/38\|C04B-028/00/6\|C04B-028/00/8\|C04B-040/00/32\|C04B-040/02/31\|C04B-2103/10\|C04B-2103/304\|C04B-2103/32\|C04B-2111/00017\|C04B-2111/00019\|C04B-2111/0075\|C04B-2111/1037\|C04B-2111/1093\|C04B-2111/29\|E01C-007/14/2\|Y02C-020/40\|Y02W-030/91	(GR1) C04B-028/00/6[RK1]; C04B-012/04[RK2]; C04B-014/04/2[RK3]; C04B-014/26[RK4]; C04B-014/28[RK5]; C04B-018/02/2[RK6]; C04B-018/08[RK7]; C04B-018/10/1[RK8]; C04B-018/14/1[RK9]; C04B-018/14/6[RK10]; C04B-022/06/4[RK11]; C04B-040/02/31[RK12]; C04B-2103/10[RK13]; C04B-2103/304[RK14]; C04B-2103/32[RK15]\|(GR1) C04B-028/00/6[RK1]; C04B-014/02[RK2]; C04B-014/06[RK3]; C04B-014/10/6[RK4]; C04B-018/08[RK5]; C04B-018/14/1[RK6]; C04B-018/14/6[RK7]; C04B-018/24/8[RK8]; C04B-020/00/8[RK9]; C04B-022/10[RK10]; C04B-040/00/28[RK11]\|(GR2) C04B-028/00/6[RK1]; C04B-012/04[RK2]; C04B-014/04/2[RK3]; C04B-014/26[RK4]; C04B-014/28[RK5]; C04B-018/08[RK6]; C04B-018/10/1[RK7]; C04B-018/14/1[RK8]; C04B-018/14/6[RK9]; C04B-022/06/4[RK10]; C04B-024/38[RK11]; C04B-040/02/31[RK12]; C04B-2103/10[RK13]; C04B-2103/304[RK14]; C04B-2103/32[RK15]\|(GR2) C04B-028/00/6[RK1]; C04B-014/02[RK2]; C04B-014/06[RK3]; C04B-014/10/6[RK4]; C04B-018/08[RK5]; C04B-018/14/1[RK6]; C04B-018/14/6[RK7]; C04B-018/24/8[RK8]; C04B-020/00/8[RK9]; C04B-040/00/28[RK10]	B28B-001/14\|B28B-001/54\|B28C-009/00/2\|C04B-012/00/5\|C04B-014/04/2\|C04B-014/06\|C04B-014/10/6\|C04B-014/26\|C04B-018/02/2\|C04B-018/08\|C04B-018/14/2\|C04B-022/00863\|C04B-022/10\|C04B-024/38\|C04B-028/00/6\|C04B-028/00/8\|C04B-040/00/32\|C04B-040/02/31\|C04B-2103/10\|C04B-2103/304\|C04B-2103/32\|C04B-2111/00017\|C04B-2111/00019\|C04B-2111/0075\|C04B-2111/1037\|C04B-2111/1093\|C04B-2111/29\|E01C-007/14/2\|Y02C-020/40\|Y02W-030/91	B28B-001/00\|C04B-012/00\|C04B-014/04\|C04B-014/06\|C04B-014/10\|C04B-014/26\|C04B-018/08\|C04B-018/14\|C04B-018/18\|C04B-022/00\|C04B-024/38\|C04B-026/00\|C04B-028/00\|C04B-040/00\|C04B-040/02\|C04B-103/10\|C04B-103/30\|C04B-103/32\|C04B-111/00	B28B-001/00\|C04B-012/00\|C04B-014/04\|C04B-014/06\|C04B-014/10\|C04B-014/26\|C04B-018/08\|C04B-018/14\|C04B-018/18\|C04B-022/00\|C04B-024/38\|C04B-026/00\|C04B-028/00\|C04B-040/00\|C04B-040/02\|C04B-103/10\|C04B-103/30\|C04B-103/32\|C04B-111/00			CN120365022\|CN120717739B	CN120365022 115400772 WHO=Examiner SELF=N CAT=A\|CN120717739B 116161526 WHO=Examiner SELF=N	KR102194390\|CN106465690\|KR102079643\|KR102043391	KR102194390 92039857 WHO=Examiner SELF=N CAT=Y CAT=A\|CN106465690 75568267 WHO=Examiner SELF=N CAT=Y CAT=A\|KR102079643 87699919 WHO=Examiner SELF=N CAT=X CAT=Y CAT=A\|KR102043391 86610040 WHO=Examiner SELF=N CAT=A		\|KR102079643; KR102194390; CN106465690; KR102043391		PENDING	(US20250250199)\|PENDING\|(WO2024/248905)\|PENDING	ALIVE	(US20250250199)\|ALIVE\|(WO2024/248905)\|ALIVE	(US20250250199)\|LEGAL DETAILS FOR US20250250199\|Actual or expected expiration date=2044-02-01\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-10-08\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US18909669\|Application date=2024-10-08\|Standardized application number=2024US-18909669\|Event publication date=2024-10-08\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2024-10-08\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2024-10-08\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 00004-Lafave_FTNPCIP\|Event publication date=2024-10-08\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 193636\|Event publication date=2024-10-08\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2024-10-08\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2024-10-08\|Event code=US/TR1RQ\|Event group=ACL Examination events\|TrackOne Accelerated Request\|Event publication date=2024-10-08\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2024-10-08\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2024-10-17\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2024-11-12\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2024-12-16\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2024-12-19\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2025-01-18\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-01-18\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-02-11\|Event code=US/TR1RQ\|Event group=ACL Examination events\|TrackOne Accelerated Request\|Event publication date=2025-03-08\|Event code=US/PDTD\|Event group=ACL Examination events\|Petition Decision Track 1 Deny\|Event publication date=2025-03-10\|Event code=US/PTDI\|Event group=OAO\|Petition Decision - Dismissed\|Event publication date=2025-08-07\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250250199\|Publication stage code=A1\|Publication date=2025-08-07\|Standardized publication number=US20250250199\|Event publication date=2025-08-07\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|(WO2024/248905)\|LEGAL DETAILS FOR WO2024/248905\|Actual or expected expiration date=2026-11-26\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-02-01\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2024/013913\|Application date=2024-02-01\|Standardized application number=2024WO-US13913\|Event publication date=2024-12-05\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2024/248905\|Publication stage code=A1\|Publication date=2024-12-05\|Standardized publication number=WO2024248905\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2025-12-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2025-12-30\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2044-02-01\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP24816062\|Event publication date=2025-01-15\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP	(WO2024/248905)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2024/248905)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2024/248905)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2024/248905)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2024/248905)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(US20250250199)\|US\|(WO2024/248905)\|WO; EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcNMYj8VpXFMrTkuDREcUBY0JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022921030&ekey=2315&xpn=US20250250199&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/18909669/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=zeXk%252BPpISmS9OMQa8KBDm8RHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(US20250250199)\|US\|(WO2024/248905)\|US	(US20250250199)\|NAME=Lafave Michael , CITY=Denvor , STATE=CO , COUNTRY=US\|(WO2024/248905)\|NAME=LAFAVE, Michael 3000 E 112th Ave. Unit 2 Denver, Colorado 80233 , COUNTRY=US	(WO2024/248905)\|US	(WO2024/248905)\|NAME=SCHELL, Jeffrey 2128 W 32nd Ave., 2nd Floor Denver, Colorado 80211 , POSTCODE=80211 , COUNTRY=US	(US20250250199)\|US\|(WO2024/248905)\|US	(US20250250199)\|NAME=Lafave Michael, CITY=Denvor, STATE=CO , COUNTRY=US\|(WO2024/248905)\|NAME=LAFAVE, Michael 3000 E 112th Ave. Unit 2 Denver, Colorado 80233, POSTCODE=80233, COUNTRY=US	(US20250250199)\|2\|(WO2024/248905)\|2	4	2					(US20250250199)\|Number of Claims: NCL=20\|Number of Drawings: NDR=2\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1,6,11,15\|Number of Independent Claims: NICL=4\|Exemplary Claim Number: ECL=1\|\|(WO2024/248905)\|Number of Claims: NCL=38\|Extended kind: EXTK=x\|	(US20250250199)\|CIP of: US18/814,312 FDD=2024-08-23 [2024US-18814312]\|Continuation of: WOUS2024/013913 FDD=2024-02-01 [2024WO-US13913] PENDING	(US20250250199)\|ENGLISH (ENG)	(US20250250199)\|Patent\|(WO2024248905)\|Patent	Titre: (US20250250199)\|Carbon-Sequestering Concrete Composition with Enhanced CO2 Absorbtion and Method of Manufacturing Thereof Résumé: (US20250250199)\|A carbon-sequestering concrete composition and method of production are disclosed. The composition comprises geopolymer binder components, aggregates, and alginate beads formed from brown algae powder through ionic gelation. The alginate beads significantly increase CO2 absorption surface area compared to algae powder, creating a matrix across the concrete surface that enhances long-term sequestration and improves durability. The beads interact synergistically with other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag, to enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The alginate beads also facilitate the dissolution of minerals like olivine, further enhancing carbon capture. The composition demonstrates superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. The method includes forming alginate beads, incorporating them into the concrete mixture, and allowing for initial hardening and drying processes that promote carbon dioxide absorption directly from the air.	29	Abstract	gpt-4o-mini	no	The article focuses on a concrete composition for carbon sequestration, which falls under materials for construction rather than accelerated weathering of minerals for CO2 capture.
30	CN201611128528	CN201611128528	CN106757119\|CN106757119	76279049	CN106757119 B 2019-02-26 [CN106757119B]\|CN106757119 A 2017-05-31 [CN106757119]	2016-12-09	2016-12-09	2019-02-26\|2017-05-31	(CN106757119B)\|2019-02-26	(CN106757119)\|2036-12-09	(CN106757119)\|One kind is for realizing CO2The electro-chemical systems that capture is sealed up for safekeeping with mineralising	(CN106757119)\|The invention belongs to the technical field of carbon resource capturing and storing and relates to a system for achieving CO2 capturing and mineralization through an electrochemical method. The system is structurally composed of three parts of a hydrodynamic force module, a reaction module and a control and display module. By means of the electrochemical technology of a steady state, a transient state and combination of the steady state and the transient state, silicate is converted into carbonate, and CO2 capturing and mineralization are achieved. The CO2 capturing and mineralization system is mainly used for relieving the increasing greenhouse effect, liquid flow drained by the system is alkaline, and treatment of ocean acidification of local areas is achieved at the same time. The system can also be used for adjusting the concentration of CO2 gas in a closed space in real time and can also serve as an auxiliary facility for emission reduction of large CO2 emission enterprises.	DALIAN INSTITUTE OF CHEMICAL PHYSICS CHINESE ACADEMY OF SCIENCES\|DALIAN UNIVERSITY OF TECHNOLOGY	(CN106757119)\|DALIAN UNIVERSITY OF TECHNOLOGY ([CN])\|DALIAN INSTITUTE OF CHEMICAL PHYSICS CHINESE ACADEMY OF SCIENCES\|(CN106757119)\|DALIAN UNIVERSITY OF TECHNOLOGY ([CN])\|DALIAN INSTITUTE OF CHEMICAL PHYSICS CHINESE ACADEMY OF SCIENCES	MAO QING\|CUI JIANMING\|HUANG YANQIANG\|LIU JIANJUN\|JING WEIYUN\|SHI YUE	(CN106757119)\|MAO QING\|CUI JIANMING\|HUANG YANQIANG\|LIU JIANJUN\|JING WEIYUN\|SHI YUE\|(CN106757119)\|MAO QING\|CUI JIANMING\|HUANG YANQIANG\|LIU JIANJUN\|JING WEIYUN\|SHI YUE	(CN106757119)\|MEI HONGYU;PATENT AGENCY CENTER OF DLUT\|Reg. Nb: 21200	(CN106757119)\|However, the application area of geological sequestration is limited, which is not only closely related to the formation of geological rock, but also has high cost for later monitoring and maintenance, and is easy to cause geological disasters if leakage occurs.\|	(CN106757119)\|1. For realizing CO2The electrochemical system for capture and mineralization sealing is characterized in that:the system comprises a fluid power module, a reaction module and a control and display module, wherein the fluid power module is connected with the reaction module and provides CO for the reaction module2The feed gas and the supplementary electrolyte and the reactant of (1); the reaction module is CO2The capture and mineralization sealing provides a reaction site, which comprises an anode chamber, a cathode chamber and a diaphragm; the anode chamber has electrodes, electrolyte, silicate and/or silicate-containing materialMinerals, electrodes and electrolyte are arranged in the cathode chamber; the anode chamber is separated from the cathode chamber by a diaphragm; the control and display module is simultaneously connected with the reaction module and the fluid power module, provides running electric power for the fluid power module, and simultaneously realizes a steady state or transient state and steady state combined electrochemical reaction mode for the reaction module, so that silicate is converted into carbonate, and CO is realized2Capturing and mineralizing and sealing; the diaphragm in the reaction module is a cation exchange membrane.\|	(CN106757119)\|In order to overcome the defects in the prior art, the invention provides a method for realizing CO2An electrochemical system for capturing, mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed; the liquid flow discharged after the system is operated is alkaline, and the treatment of ocean acidification problems in a designated area can be realized to a certain extent.\|The system consists of a fluid power module, a reaction module and a control and display module.\|	(CN106757119)\|MINERALIZATION SEALING(100,16)\|SAFEKEEPING(100,4)\|REACTION MODULE(86,30)\|MINERALIZATION SEQUESTRATION(84,10)\|CO2THE MINERALIZATION(79,1)\|OCEAN ACIDIFICATION TREATMENT(75,1)\|GEOLOGICAL SEQUESTRATION(64,2)\|GEOLOGICAL ROCK FORMATION(61,1)\|GEOLOGICAL ROCK(60,1)\|CATHODE CHAMBER(57,8)\|ANODE COMPARTMENT(57,2)\|GEOLOGICAL DISASTER(57,2)\|ANODE CHAMBER(56,9)\|OCEAN ACIDIFICATION(53,3)\|ELECTROLYTE(52,9)\|SILICATE(49,16)\|MIXED GAS2THE(49,2)\|LATE MONITORING(45,1)\|DIAPHRAGM(44,7)\|CO2A CONCENTRATION SENSOR(44,3)\|REACTION MODULE2THE(44,2)\|CARBON RESOURCE CAPTURE(44,1)\|MATERIALMINERAL(44,1)\|SINE WAVE(42,4)\|NATURAL ORE(42,1)\|REGIONAL AREA OCEAN ACIDIFICATION(41,1)\|EQUILIBRIUM TRANSPORT(37,1)\|TRANSIENT(36,7)\|REAGENT(33,7)\|SUPPLEMENT ELECTROLYTE(33,3)\|SENSOR DEVICETHE RESPONSE(31,1)\|FLUID POWER MODULE(29,14)\|AUXILIARY EQUIPMENT(29,1)\|ENTERPRISE EMISSION REDUCTION(27,1)\|DEFECT(26,1)\|CO2CAPTURE(25,1)\|REACTIONWHEN(25,1)\|REACTION SITE(24,3)\|TRIANGULAR WAVE(24,3)\|CO2CO(24,2)\|ALKALINITY(23,1)\|OLIVINE(22,2)\|ELECTROCHEMICAL REACTION MODE(21,2)\|CATION EXCHANGE MEMBRANE(20,2)\|ENCLOSURE(20,1)\|FLUID DYNAMIC MODULE(20,1)\|REACTOR(19,5)\|STEADY STATE(18,18)\|AIR2THE ABSORPTION(18,5)\|ELECTRICAL POWER(18,5)\|VOLTAGE INFORMATION(18,3)\|LIQUID STREAM(18,1)\|SLEIPNER GEOLOGICAL SEQUESTRATION PROJECT(18,1)\|COMBINED ELECTROCHEMICAL REACTION MODE(17,2)\|MICROBIAL ELECTROCHEMICAL CO2A CAPTURE(17,1)\|OCEAN ACIDIFICATION CO2THE(16,1)\|REACTION MODULE OPERATION MODE(15,7)\|SQUARE WAVE(15,4)\|WORKING CURRENT DENSITY(15,4)\|GEOLOGICAL SEQUESTRATION APPLICATION AREA(15,1)\|CO2AN ELECTROLYTIC CAPTURE(13,1)\|ELECTROCHEMICAL PROCESS2THE CAPTURE(13,1)\|FLUID MOVEMENT(13,1)\|POROUS ELECTRODE STRUCTURE(12,2)\|CO2THE ELECTROCHEMICAL CAPTURE(12,1)\|ELECTROCHEMICAL CO2THE CAPTURE(12,1)\|GEOLOGICAL DISASTER RISK(12,1)\|LARGE SCALE CO2DISCHARGE(12,1)\|SILICATE MINERALS2A CAPTURE(12,1)\|DENSITY2THE ABSORPTION(11,2)\|CO2SUBSEQUENT ELECTRODIALYSIS(11,1)\|ELECTROCHEMICAL METHOD2COMPARED(11,1)\|SILICATE ROCK RESERVE(11,1)\|SILICATE INCORPORATION(10,2)\|ANODE CHAMBER2THE(10,1)\|INTO2THE TRAPPING(10,1)\|OCEAN SEQUESTRATION(10,1)\|POROUS TEFLON MEMBRANE(10,1)\|REALIZING CO2ELECTROCHEMICAL(10,1)\|LIQUID LEVEL SENSOR(9,3)\|TEMPERATURE SENSOR(9,3)\|SENSING DEVICE(8,12)\|PRESSURE SENSOR(8,3)\|FLAT ELECTRODE STRUCTURE(8,2)\|GREENHOUSE EFFECT(8,2)\|CO2HAS EMISSION(8,1)\|DENSITIES2THE ABSORPTION(8,1)\|MARKET MATURITY(8,1)\|RESIDENTIAL BUILDING(8,1)\|SEQUESTRATION SITE(8,1)\|SILICATE NONADDITION(8,1)\|WORKING MEDIUM2THE MINERALIZATION PRODUCT(8,1)\|DISPLAY DEVICE(7,6)\|CALCIUM SILICATE INTRODUCTION(7,2)\|ELECTROLYTE MOLTEN SALT(7,2)\|GEOLOGICAL STORAGE(7,2)\|PLATINUM SHEET(7,2)\|ABSORPTION ELECTROLYSIS(7,1)\|ANHYDROUS LIF(7,1)\|CCS CORE(7,1)\|DEMONSTRATION PROJECT(7,1)\|FLUE GAS2BY(7,1)\|MEMBRANE ELECTROLYSIS(7,1)\|MICROPOROUS MEMBRANE(7,1)\|NORTH SEA NORWEGIAN(7,1)\|POTASSIUM FELDSPAR(7,1)\|SEQUESTRATION2HIGH CONCENTRATION COMPRESSION(7,1)\|SILICATE SPECIES GRAPH(7,1)\|SIGNAL CHANGE FREQUENCY RANGE(6,3)\|ANODE INCORPORATIONTHE ACIDIFICATION DEGREE(6,1)\|ANODE PH(6,1)\|APPLICATION AREA(6,1)\|AQUEOUS CARBONATE CAPTURE(6,1)\|CATHODE COMPARTMENT(6,1)\|CO2AFTER CALCIUM SILICATE(6,1)\|CO2CHEMICAL REACTION(6,1)\|ELECTRODIALYSIS2BY AQUEOUS SOLUTION(6,1)\|FIREPROOF COATING(6,1)\|FOSSIL FUEL COMBUSTION(6,1)\|GEOLOGICAL SEALING(6,1)\|INORGANIC ASH(6,1)\|INTERNATIONAL SOCIETY CONCERN(6,1)\|LI2CO3THE MOLAR RATIO(6,1)\|LIQUID FLOW(6,1)\|METHANEDIONE ELECTROCHEMICAL REDUCTION(6,1)\|OCEAN SEALING(6,1)\|ORGANIC WASTEWATER(6,1)\|POSITIVE PRESSURE2SOLVENT(6,1)\|PURITY CO2(6,1)\|REGENERATED CAPTURE SOLUTION(6,1)\|RELEASING TOWER(6,1)\|SEWAGE TREATMENT CO2THE(6,1)\|BICARBONATE(5,2)\|OCEAN STORAGE(5,2)\|TRANSPORTATION(5,2)\|ANION EXCHANGE MEMBRANE(5,1)\|CO2THE SEQUESTRATION(5,1)\|CO2THE SOLUTION(5,1)\|CONDITION2THE(5,1)\|DIOSMECTITE(5,1)\|DISCLOSED2THERE(5,1)\|FOAM COPPER(5,1)\|FOAM NICKEL(5,1)\|GAS REALTIME ADJUSTING(5,1)\|INTERMITTENT DISCHARGE MODE(5,1)\|MICROBIAL NUTRIENT SOURCE(5,1)\|MINERALIZATION PRODUCTION(5,1)\|NATURALLY OCCURRING SILICATE(5,1)\|NI ALLOY(5,1)\|NONMETAL(5,1)\|SYSTEM2THE AIR(5,1)\|SYSTEMTHE ANGULAR WAVE SIGNAL(5,1)\|MAGNESIUM SILICATE(4,3)\|STEADY STATE OPERATION MODE(4,3)\|TRANSIENT STATE OPERATION MODE(4,3)\|COMBINED OPERATION MODE(3,4)\|ABSORPTION STEADY STATE BEHAVIOR(3,1)\|AGALMATOLITE(3,1)\|ALKALINE EARTH OXIDE(3,1)\|ALUMINATE(3,1)\|ANOLYTE(3,1)\|ASBESTOS(3,1)\|BASALT(3,1)\|\|(CN106757119)\|MINERALIZATION SEALING(100,18)\|SAFEKEEPING(100,4)\|REACTION MODULE(76,31)\|CO2THE MINERALIZATION(70,1)\|OCEAN ACIDIFICATION TREATMENT(67,1)\|MINERALIZATION SEQUESTRATION(61,9)\|ELECTROCHEMICAL METHOD2THE(57,1)\|GEOLOGICAL SEQUESTRATION(56,2)\|GEOLOGICAL ROCK FORMATION(54,1)\|GEOLOGICAL ROCK(53,1)\|CATHODE CHAMBER(51,8)\|GEOLOGICAL DISASTER(51,2)\|ANODE CHAMBER(50,9)\|ANODE COMPARTMENT(50,2)\|ELECTROLYTE(47,9)\|OCEAN ACIDIFICATION(47,3)\|SILICATE(43,16)\|INVENTION2CAPTURE SEAL(41,1)\|CO2THE AUXILIARY EQUIPMENT(40,1)\|LATE MONITORING(40,1)\|CO2A CONCENTRATION SENSOR(39,3)\|REACTION MODULE2THE(39,2)\|MATERIALMINERAL(39,1)\|NATURAL ORE(38,1)\|SINE WAVE(37,4)\|REGIONAL AREA OCEAN ACIDIFICATION(36,1)\|DIAPHRAGM(34,7)\|TRANSIENT(33,7)\|SENSING DEVICEREACTION RESPONSE(31,1)\|MICROPOROUS MEMBRANE(30,2)\|SUPPLEMENT ELECTROLYTE(29,3)\|FLUID POWER MODULE(28,14)\|DISCHARGE ENTERPRISE EMISSION REDUCTION(26,1)\|REAGENT(25,6)\|ALKALESCENCE(23,1)\|DEFECT(23,1)\|CARBON RESOURCE(22,2)\|REACTION SITE(21,3)\|NONMETAL(20,2)\|ELECTRICAL POWER(19,6)\|TRIANGULAR WAVE(19,4)\|OLIVINE(19,2)\|EQUILIBRIUM(19,1)\|ELECTROCHEMICAL REACTION MODE(18,2)\|REACTOR(17,5)\|FLUID DYNAMIC MODULE(17,1)\|STABLEIN(17,1)\|AIR2THE ABSORPTION(16,5)\|MIXED GAS(16,3)\|VOLTAGE INFORMATION(16,3)\|SLEIPNER GEOLOGICAL SEQUESTRATION PROJECT(16,1)\|SYSTEM RELIEF LIQUOR STREAM(16,1)\|STEADY STATE(15,17)\|REACTION MODULE OPERATION MODE(15,8)\|COMBINED ELECTROCHEMICAL REACTION MODE(15,2)\|CLOSING SPACE(15,1)\|MICROBIAL ELECTROCHEMICAL CO2A CAPTURE(15,1)\|DISPLAY MODULE THREE(14,1)\|OCEAN ACIDIFICATION CO2THE(14,1)\|SQUARE WAVE(13,4)\|WORKING CURRENT DENSITY(13,4)\|GEOLOGICAL SEQUESTRATION APPLICATION AREA(13,1)\|CO2AN ELECTROLYTIC CAPTURE(12,1)\|COUNTER POWER(12,1)\|ELECTROCHEMICAL PROCESS2THE CAPTURE(12,1)\|CATION EXCHANGE MEMBRANE(11,2)\|POROUS ELECTRODE STRUCTURE(11,2)\|CO2THE ELECTROCHEMICAL CAPTURE(11,1)\|ELECTROCHEMICAL CO2THE CAPTURE(11,1)\|GEOLOGICAL DISASTER RISK(11,1)\|SILICATE MINERALS2A CAPTURE(11,1)\|DENSITY2THE ABSORPTION(10,2)\|CO2SUBSEQUENT ELECTRODIALYSIS(10,1)\|ELECTROCHEMICAL METHOD2COMPARED(10,1)\|LIQUID LEVEL SENSOR(8,3)\|TEMPERATURE SENSOR(8,3)\|ANODE CHAMBER2THE(8,1)\|INTO2THE TRAPPING(8,1)\|OCEAN SEQUESTRATION(8,1)\|POROUS TEFLON MEMBRANE(8,1)\|REALIZING CO2ELECTROCHEMICAL(8,1)\|PRESSURE SENSOR(7,3)\|FLAT ELECTRODE STRUCTURE(7,2)\|GREENHOUSE EFFECT(7,2)\|ACID ROCK CRUSTTHE RESERVE(7,1)\|CO2HAS EMISSION(7,1)\|DENSITIES2THE ABSORPTION(7,1)\|MARKET MATURITY(7,1)\|SEQUESTRATION SITE(7,1)\|SILICATE NONADDITION(7,1)\|WORKING MEDIUM2THE MINERALIZATION PRODUCT(7,1)\|DISPLAY DEVICE(6,6)\|CALCIUM SILICATE INTRODUCTION(6,2)\|ELECTROLYTE MOLTEN SALT(6,2)\|GEOLOGICAL STORAGE(6,2)\|PLATINUM SHEET(6,2)\|ABSORPTION ELECTROLYSIS(6,1)\|ANHYDROUS LIF(6,1)\|CCS CORE(6,1)\|DEMONSTRATION PROJECT(6,1)\|FLUE GAS2BY(6,1)\|MEMBRANE ELECTROLYSIS(6,1)\|NORTH SEA NORWEGIAN(6,1)\|POTASSIUM FELDSPAR(6,1)\|SEQUESTRATION2HIGH CONCENTRATION COMPRESSION(6,1)\|SILICATE SPECIES GRAPH(6,1)\|SIGNAL CHANGE FREQUENCY RANGE(5,3)\|ANODE PH(5,1)\|APPLICATION AREA(5,1)\|AQUEOUS CARBONATE CAPTURE(5,1)\|CATHODE COMPARTMENT(5,1)\|CO2AFTER CALCIUM SILICATE(5,1)\|CO2CHEMICAL REACTION(5,1)\|ELECTRODIALYSIS2BY AQUEOUS SOLUTION(5,1)\|FIREPROOF COATING(5,1)\|GAS REALTIME REGULATION(5,1)\|GEOLOGICAL SEALING(5,1)\|INORGANIC ASH(5,1)\|INTERNATIONAL SOCIETY CONCERN(5,1)\|LI2CO3THE MOLAR RATIO(5,1)\|LIQUID FLOW(5,1)\|METHANEDIONE ELECTROCHEMICAL REDUCTION(5,1)\|OCEAN SEALING(5,1)\|ORGANIC WASTEWATER(5,1)\|POSITIVE PRESSURE2SOLVENT(5,1)\|PURITY CO2(5,1)\|REGENERATED CAPTURE SOLUTION(5,1)\|RELEASING TOWER(5,1)\|SEWAGE TREATMENT CO2THE(5,1)\|BICARBONATE(4,2)\|OCEAN STORAGE(4,2)\|TRANSPORTATION(4,2)\|ANION EXCHANGE MEMBRANE(4,1)\|CALCIUM SILICATE INCORPORATION(4,1)\|CO2THE SEQUESTRATION(4,1)\|CO2THE SOLUTION(4,1)\|CONDITION2THE(4,1)\|DIOSMECTITE(4,1)\|DISCLOSED2THERE(4,1)\|FLOWTHE(4,1)\|FOAM COPPER(4,1)\|FOAM NICKEL(4,1)\|INTERMITTENT DISCHARGE MODE(4,1)\|MICROBIAL NUTRIENT SOURCE(4,1)\|MINERALIZATION PRODUCTION(4,1)\|NATURALLY OCCURRING SILICATE(4,1)\|NI ALLOY(4,1)\|SYSTEM2THE AIR(4,1)\|COMBINED OPERATION MODE(3,4)\|MAGNESIUM SILICATE(3,3)\|STEADY STATE OPERATION MODE(3,3)\|TRANSIENT STATE OPERATION MODE(3,3)\|ABSORPTION STEADY STATE BEHAVIOR(3,1)\|AGALMATOLITE(3,1)\|ALKALINE EARTH OXIDE(3,1)\|ALUMINATE(3,1)\|	(CN106757119)\|1. For realizing CO2The electrochemical system for capture and mineralization sealing is characterized in that:\|the system comprises a fluid power module, a reaction module and a control and display module, wherein the fluid power module is connected with the reaction module and provides CO for the reaction module2The feed gas and the supplementary electrolyte and the reactant of (1); the reaction module is CO2The capture and mineralization sealing provides a reaction site, which comprises an anode chamber, a cathode chamber and a diaphragm; the anode chamber has electrodes, electrolyte, silicate and/or silicate-containing materialMinerals, electrodes and electrolyte are arranged in the cathode chamber; the anode chamber is separated from the cathode chamber by a diaphragm; the control and display module is simultaneously connected with the reaction module and the fluid power module, provides running electric power for the fluid power module, and simultaneously realizes a steady state or transient state and steady state combined electrochemical reaction mode for the reaction module, so that silicate is converted into carbonate, and CO is realized2Capturing and mineralizing and sealing; the diaphragm in the reaction module is a cation exchange membrane.\|2. A method for the realization of CO according to claim 12The electrochemical system for trapping and mineralizing and sealing is characterized in that the electrode material comprises a simple substance, an alloy or a compound formed by other non-metallic elements, wherein the simple substance or the alloy contains Pt, Re, Pd, Rh, Mo, W, Nb, Ru, Ir, Sn, Mn, Fe, Co, Ni, Cu, Ag and C.\|3. A method for the realization of CO according to claim 1 or 22The electrochemical system for capture and mineralization sealing is characterized in that the anode is of a flat electrode structure or a porous electrode structure.\|4. A method for the realization of CO according to claim 1 or 22Electrochemical system for capture and mineralization sequestration characterized in that said anodic compartment is treated with CO2CO in mixed gas2The concentration range of (A) is between 0.050% and 99.995%.\|5. A method for the realization of CO according to claim 32Electrochemical system for capture and mineralization sequestration characterized in that said anodic compartment is treated with CO2CO in mixed gas2The concentration range of (A) is between 0.050% and 99.995%.\|6. A method for the realization of CO according to claim 1 or 2 or 52Electrochemical system for capture and mineralization sequestration, characterised by the reactionWhen the module operation mode is a steady state, the working current density range is 0.075mA/cm2～2A/cm2To (c) to (d); when the operation mode of the reaction module is transient, sine wave, square wave and triangular wave signals of current or voltage are loaded to the system, and the change frequency range of the signals is 1000 Hz-0.1 Hz.\|7. A method for the realization of CO according to claim 32The electrochemical system for capture and mineralization sealing is characterized in that when the operation mode of the reaction module is steady state, the working current density range is 0.075mA/cm2～2A/cm2To (c) to (d); when the operation mode of the reaction module is transient, sine wave, square wave and triangular wave signals of current or voltage are loaded to the system, and the change frequency range of the signals is 1000 Hz-0.1 Hz.\|8. A method for the realization of CO according to claim 42The electrochemical system for capture and mineralization sealing is characterized in that when the operation mode of the reaction module is steady state, the working current density range is 0.075mA/cm2～2A/cm2To (c) to (d); when the operation mode of the reaction module is transient, sine wave, square wave and triangular wave signals of current or voltage are loaded to the system, and the change frequency range of the signals is 1000 Hz-0.1 Hz.\|9. A process for the realization of CO according to claim 1 or 2 or 5 or 7 or 82The electrochemical system for capture and mineralization sealing is characterized in that the control and display module comprises a sensing device, a system control device and a display device; wherein the sensing device comprises H2、O2、CO2A concentration sensor, a temperature sensor, a liquid level sensor and a pressure sensor; the display device is used for displaying temperature, pressure and O in system operation2Concentration, H2Concentration, CO2Concentration, liquid level, current, voltage information; the system control device supplies electric power to the sensor device and controls fluid movement according to the response of the sensor deviceThe force module provides reactants and supplementary electrolyte for the reactor; on the other hand, a digital signal processor in the system control device controls the operation of the reactor, and provides a steady-state operation mode, a transient-state operation mode or a steady-state and transient-state combined operation mode for the system.\|10. A method for the realization of CO according to claim 32The electrochemical system for capture and mineralization sealing is characterized in that the control and display module comprises a sensing device, a system control device and a display device; wherein the sensing device comprises H2、O2、CO2A concentration sensor, a temperature sensor, a liquid level sensor and a pressure sensor; the display device is used for displaying temperature, pressure and O in system operation2Concentration, H2Concentration, CO2Concentration, liquid level, current, voltage information; on one hand, the system control device provides electric power for the sensing device and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a digital signal processor in the system control device controls the operation of the reactor, and provides a steady-state operation mode, a transient-state operation mode or a steady-state and transient-state combined operation mode for the system.	(CN106757119)\|TECHNICAL FIELD\|[0002] The invention belongs to the technical field of capture and storage of carbon resources, and relates to a method for realizing CO2Electrochemical system for capture and mineralization sequestration\|BACKGROUND ART\|[0004] CO excessively discharged in China2Mainly from fossil fuel combustion, e.g. for power generation, but also from small dispersed sources, e.g. automobile engines, and combustion in residential and commercial buildingsA furnace; in addition to this, CO2Also in the refining of certain mineral resources. Currently, excessive emission of CO2Has led to an increasingly severe greenhouse effect, due to the large part of CO2Gas is absorbed by the ocean, which makes the ocean acidification problem increasingly serious. The concern of the international society on climate change leads to the emergence of the framework convention of climate change of the united nations, and further promotes CO2Development of capture and sequestration technology (CCS) technology.\|[0005] CCS technology generally includes three major components of capture, transport and containment. First, the capture step is to capture CO2Separated from other gaseous products. Such as combustion processes in power plants, separation techniques may be employed to capture CO after combustion2Or decarbonizing the fuel prior to combustion. Secondly, in order to capture CO2Transport to CO2The source is far away from the appropriate sequestration site, requiring transportation steps to be taken. Captured CO for ease of transportation and sequestration2High concentration compression is typically performed by the capture device. Last CO2The sequestration process is the core of CCS technology, determining the overall process cost and process complexity. Currently, CO2The sealing technology comprises three types of geological sealing, ocean sealing and mineralization sealing, and the technology is greatly different from the maturity of the market. Geological sequestration technology is relatively mature, and currently, industrial demonstration projects are available, such as: the Norwegian North sea Sleipner geological sequestration project has successfully injected 1000 million tons of CO into the ground2. However, the application area of geological sequestration is limited, which is not only closely related to the formation of geological rock, but also has high cost for later monitoring and maintenance, and is easy to cause geological disasters if leakage occurs.\|[0006] Ocean sequestration and mineralization sequestration are currently only in the research, development, or demonstration stages. Among these, the mineralization sequestration technology has great potential to develop, which mainly utilizes the basic or alkaline earth oxides, such as magnesium oxide and calcium oxide, present in naturally occurring silicate rocks to sequester CO2And (5) curing. These substances are mixed with CO2Chemical reactions produce compounds such as magnesium carbonate and calcium carbonate. The advantages of mineralization and sequestration are as follows: (1) wide raw material sourceAnd 4. preparing the compound. On the one hand, the reserves of silicate rock in the crust are enormous, while these oxides may also be present in certain industrial wastes, such as stainless steel slag and mineral ash; (2) CO 22After mineralization, the mineral is not released into the atmosphere, compared with geological storage and ocean storage, the mineral is free from subsequent monitoring and maintenance cost, and the storage risk is small; (3) the mineralized carbonate product has wide application, can be used as building materials and fireproof coatings, is also an important chemical raw material, and is widely applied to the industries of chemical industry, glass, paper making and the like.\|[0007] CO presently disclosed2There are two main types of capture and mineralization sequestration techniques. One is achieved by chemical methods, while the other is based on electrochemical methods. The former is mostly carried out at high temperature or high pressure, and the system structure is complex. For example, Olsen Espen discloses the use of metal oxide salt solutions to absorb CO at temperatures between 600 ℃ and 1600 ℃2The technology and process of (CN 102448581A, US 20120128559). Terasaka et al (chem. Eng. Technol.2006, 29No 9, pp. 1118-4) Absorption of CO as a working medium2The mineralization product is Li2CO3And Li2SiO3In the form of suspended solid particles. US2005036932 discloses an absorption and removal of CO from flue gas2By bubbling the exhaust gas through a stream containing CaO and/or Ca (OH)2Of solid particles of (a) so that CO in the exhaust gas is present2Conversion to CaCO3. CN 102491795A discloses CO at 150-350 deg.C2Under the condition that the partial pressure is not lower than 1.0MPa, the potassium feldspar is used for leading CO to be treated2A method for producing a potassium-rich solution by mineralization; CN 102895847A discloses that CO is introduced into2The trapping method comprises introducing molten alkali metal, alkaline earth metal, transition metal carbonate, silicate, borate, oxide, hydroxide, nitrate, aluminate and their mixture into the reactor for absorption electrolysis. CN 103111161A discloses a larger scale CO2Capture process by CO with positive pressure2Solvent capture of CO in a capture column2Supersaturated CO2The solution enters a releasing tower again for extraction and concentration.CO based electrochemical process2The capture and conversion process is relatively simple and the operating environment is relatively mild, CN 101670236A discloses recovery of CO by aqueous carbonate capture and electrodialysis2By aqueous solution capture of CO2Subsequent electrodialysis to form CO-rich2Liquid flow and regenerated capture solution. CN 102351310A discloses microbial electrochemical CO2A capture system using organic wastewater as a microbial nutrient source in CO2The problem of sewage treatment is considered while the sewage is captured. CN 102978653A discloses a mineralized CO2The membrane electrolysis method for coproducing strong acid is characterized by that its mineralized raw material is nitrate or sulfate, and its product is carbonate and nitric acid. CN 105420751 a discloses a method for preparing hydrocarbons by electrochemical reduction of carbon dioxide, which uses alkali metal carbonate (bicarbonate), sulfate, phosphate (bicarbonate), etc. as substances and electrolyte, and is characterized in that an organic solvent is introduced into an electrolyte system. Unlike electrochemical capture in aqueous systems, CN 103590064 a discloses the use of anhydrous LiF and Li2CO3The molar ratio (0.5-1.5): 1, uniformly mixing, adding an additive to prepare electrolyte molten salt, placing the electrolyte molten salt in an electrolytic cell, heating to 690-700 ℃, and introducing CO2An electrolytic capture method. Wherein the cathode material is Ni or Ti, and the anode material is Pt, Fe-Ni alloy or Fe-Ni-Al2O3And (3) alloying.\|DISCLOSURE\|[0008] Disclosure of Invention\|[0009] In order to overcome the defects in the prior art, the invention provides a method for realizing CO2An electrochemical system for capturing, mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed; the liquid flow discharged after the system is operated is alkaline, and the treatment of ocean acidification problems in a designated area can be realized to a certain extent.\|[0010] Can realize CO2The technical scheme of the electrochemical system for capturing, mineralizing and sealing up comprises the following steps:\|[0011] the system comprises a fluid power module, a reaction module and a control and display module, wherein the fluid power module is connected with the reaction module and provides CO for the reaction module2The feed gas and the supplementary electrolyte and the reactant of (1); the reaction module is CO2The capture and mineralization sealing provides a reaction site, which comprises an anode chamber, a cathode chamber and a diaphragm; the anode chamber is internally provided with an electrode, electrolyte, silicate and/or mineral containing silicate, and the cathode chamber is internally provided with an electrode and electrolyte; the anode chamber is separated from the cathode chamber by a diaphragm; the control and display module is simultaneously connected with the reaction module and the fluid power module, provides running electric power for the fluid power module, and simultaneously realizes a steady state or transient state and steady state combined electrochemical reaction mode for the reaction module, so that silicate is converted into carbonate, and CO is realized2Capture and mineralize and seal up.\|[0012] The diaphragm in the reaction module comprises an anion-exchange membrane, a cation-exchange membrane or a microporous membrane (such as a porous polytetrafluoroethylene membrane); the electrode material comprises simple substances, alloys or compounds formed by other nonmetal elements containing Pt, Re, Pd, Rh, Mo, Wo, Nb, Ru, Ir, Sn, Mn, Fe, Co, Ni, Cu, Ag and C. The silicate includes all compounds or mixtures containing silicon, oxygen and other chemical elements (such as aluminum, iron, calcium, magnesium, manganese, potassium, sodium, barium, copper, zinc, lead, tin). The silicate-containing mineral includes olivine, serpentine, basalt, asbestos, mica, talc, kaolinite, montmorillonite, zeolite, agalmatolite, tourmaline, pyroxene, and hornblende containing the above silicate components.\|[0013] The anode is of a flat electrode structure or a porous electrode structure.\|[0014] CO treated in the anode chamber2The concentration range of the mixed gas is between 0.050% and 99.995%.\|[0015] When the operation mode of the reaction module is steady state, the working current density range is 0.075mA/cm2～2 A/cm2To (c) to (d); when the operation mode of the reaction module is transient, a sine wave, a square wave and a three wave of current or voltage are loaded on the systemThe angular wave signal has a variation frequency range of 1000 Hz-0.1 Hz.\|[0016] The control and display module comprises a sensing device, a system control device and a display device; wherein the sensing device comprises H2、O2、CO2A concentration sensor, a temperature sensor, a liquid level sensor and a pressure sensor; the display device is used for displaying temperature, pressure and O in system operation2Concentration, H2Concentration, CO2Concentration, level, current, voltage information; on one hand, the system control device provides electric power for the sensing device and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a digital signal processor in the system control device controls the operation of the reactor, and provides a steady-state operation mode, a transient-state operation mode or a steady-state and transient-state combined operation mode for the system.\|[0017] CO of system treatment2The concentration range of the gas is wide, namely high-concentration CO can be realized2(99.99%) conversion can also be used for trace amounts of CO in air2(ppm level) conversion, System CO2The transformation scale of (2) is controllable and modularization is easy to realize. The discharged product of the system after operation is environment-friendly and alkaline, and the system can realize CO2The problem of ocean acidification which is becoming more serious at present can be simultaneously relieved while the capture and the mineralization are sealed.\|[0018] The invention realizes CO by adopting an electrochemical method2Compared with the application of physical methods (including geological storage and ocean storage), the technology does not need to be monitored in the later period and has no risk of geological disasters. Compared with the existing applied chemical method to realize CO2Compared with the technology of capture and mineralization sealing, the invention applies the electrochemical method without high temperature and high pressure reaction environment, the reaction can be carried out at normal temperature and normal pressure, the system has simple structure and low energy consumption, and is easy to realize modular design and has huge application prospect.\|DRAWINGS DESCRIPTION\|[0020] FIG. 1 is CO2The structure of the electrochemical capture and mineralization sealing system is shown schematically.\|[0021] FIG. 2 is introduction of calcium silicate to CO in air2The absorption efficiency and the system cell pressure.\|[0022] FIG. 3 is a graph of silicate species vs. CO in the air of the system2The effect of the absorption effect of (c).\|[0023] FIG. 4 is a graph of the system versus CO in air at different current densities2The absorption effect of (1).\|[0024] Wherein (a) is CO2A time-dependent profile; (b) after 3 hours, CO2Concentration profile with system power.\|[0025] FIG. 5 shows 4mA cm of electrode material at room temperature for a system-2For CO in air under the condition2The effect of absorption.\|[0026] Wherein (a) is CO2The change in concentration over time; (b) is the change of the system tank pressure with time.\|[0027] FIG. 6 shows the system operating under unsteady state current conditions for CO in air2The absorption effect of (1).\|[0028] Wherein (a) is the variation of the system current with time; (b) is CO2The change in concentration with time.\|[0029] FIG. 7 is a graph of the system versus CO in air at low current density2The absorption effect of (1).\|[0030] FIG. 8 is a graph of system for high purity CO at high current density2The absorption effect of (1).\|INVENTION MODE\|[0031] Detailed Description\|[0032] To further illustrate the invention, the following examples are presented to describe CO2The electrochemical capture and containment system is not intended to limit the scope of the invention.\|INVENTION MODE\|[0033] Example 1: CO 22Electrochemical capture and containment system architecture\|[0034] FIG. 1 shows CO2And (3) an electrochemical capture and mineralization sequestration system structure. The system consists of a fluid power module, a reaction module and a control and display module. The fluid power module is connected with the reaction module and can be provided with CO2May also be supplemented with supporting electrolytes and reactants. The control and display module is simultaneously connected with the reaction module and the fluid power module, and the system controller provides electric power for the sensing device on one hand and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a Digital Signal Processor (DSP) in the controller can control the operation of the reactor, provide steady-state, transient-state, steady-state and transient-state combined operation modes for the system and realize shutdown operation. The reaction module is the core component of the system and is CO2The capture and mineralization sealing provides a reaction site, and the structure of the device consists of an anode chamber, a cathode chamber and a diaphragm. The anode chamber and the cathode chamber are respectively provided with an anode, an anolyte, a cathode and a catholyte, wherein the anode chamber contains silicate.\|INVENTION MODE\|[0035] Example 2: CO 22The electrochemical capture and mineralization sequestration system is the same as example 1, which compares the addition or non-addition of silicate to the system CO2Absorption efficiency and emission of products.\|[0036] FIG. 2 shows electrochemical CO with and without silicate minerals2A capture and mineralization sealing system with a current density of 2mA cm-2Under the condition, the system can be used for treating CO in the air2The absorption effect and the system tank pressure. It can be seen that the introduction of calcium silicate is for CO2The absorption and system power consumption effects of (1) produced significant results after 100 minutes, calcium silicate containing system exhaust gas CO2The concentration is relatively low. Table 1 shows the effect of silicate incorporation on the pH of the effluent after 8 hours of operation of the system, which is seen in calcium silicate incorporationThe acidification degree of the anode discharge product is obviously reduced.\|[0037] TABLE 1 Effect of silicate incorporation on the pH of the anode and cathode compartments\|[0038] \|INVENTION MODE\|[0039] Example 3: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, in this example, silicate species are compared to system CO2The absorption efficiency of (a).\|[0040] FIG. 3 shows the reaction at CO2After calcium silicate, magnesium silicate, aluminum silicate and sodium silicate are introduced into the electrochemical capture and mineralization sealing system, the system can be used for treating CO in the air at room temperature2Comparison of absorption effects. The reaction module is operated in a steady-state constant current mode in the system operation, and the current is 2 mA-cm-2. It can be seen that the type of silicate affects the system CO2Transient and steady state behavior of the absorption. System Pair CO introducing aluminum silicate and magnesium silicate 1 hour after system startup2The absorption effect is inferior to that of the system containing calcium silicate and sodium silicate. After 3 hours of operation, the system had entered steady state, with systems employing magnesium silicate for CO2The absorption effect of (A) is inferior to that of the other three silicates.\|INVENTION MODE\|[0041] Example 4: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, this example considers the current density to the system CO2The effect of the absorption effect.\|[0042] Experiment researches electrochemical CO2The capture and mineralization sealing system has different current densities of 0.5 mA-cm-2～6mA·cm-2For CO in air when silicate A is contained2The absorption effect of (2) is shown in FIG. 4 (a). It can be seen that as the current density increases, the mixed gas is dischargedCO2Reduced content, system to CO2The time for absorption to reach stability increases. However, the system is for CO in air2Is not proportional to the output of system power, and fig. 4(b) shows CO in the system exhaust2The concentration of (A) is varied with the system power and is 0.5mA cm-2～6mA·cm-2In the current density range, CO2The increase in processing power of (a) is accompanied by an exponential increase in system power.\|INVENTION MODE\|[0043] Example 5: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, this example compares the electrode material to the system CO2The effect of the absorption effect.\|[0044] FIG. 5(a) shows the CO content of the system in air when the anode electrode materials are copper sheet, platinum sheet, foam copper and foam nickel respectively2And (5) comparing the absorption effect. Wherein, the copper sheet and the platinum sheet are flat electrodes, and the foam copper and the foam nickel are porous electrodes. It can be seen that under the premise of the same current density, the change of the electrode material can be used for CO in the air2The absorption effect of (2) has an influence, and the system tank pressure changes remarkably. When the foam nickel with the porous structure is used as the anode, the power consumption is minimum, and the energy is saved most.\|INVENTION MODE\|[0045] Example 6: CO 22The structure of the electrochemical capture and mineralization sequestration system is the same as that of the embodiment 1, and the reaction module in the embodiment operates in a transient state and steady state combined operation mode.\|[0046] FIG. 6 shows the system pairs and CO in air for the transient and steady state combined operation mode of the reaction module2Wherein the area of the electrode used for the anode in the reaction module is 4cm2. FIG. 6(a) shows the change of the current of the reaction module with time, the system is at 6mA (1.5mA cm) in 0-5 min-2) On the basis, 2mA (0.5mA cm) is loaded-2) The frequency of the current change is 1 Hz; changing the frequency of the loading alternating current signal to 0.1Hz in the following 25 minutes; in thatThe frequency change is increased to 1000Hz in 30-55 minutes, and in the last 25 minutes, the system is in an intermittent discharge mode, namely, the system stops for 1 minute every 5 minutes of operation. FIG. 6(b) shows the system outlet CO in the operating mode as shown in FIG. 6(a)2The concentration of (c) is varied. It can be seen that in the transient and steady state combined operation mode, the system still works against CO in air2Has obvious effect on absorption.\|INVENTION MODE\|[0047] Example 7: CO 22The structure of the electrochemical capture and mineralization sequestration system is the same as that of the embodiment 1, and the embodiment considers that the system is used for CO in the air when the current is low2Absorption effect of\|[0048] FIG. 7 shows the use of 0.075mA cm in the reaction module-2System for CO in air2The absorption effect of (1). The results show that the system is in this mode of operation, after 20 minutes, towards CO2The absorption enters a stable operation state, and the CO in the air can be reduced after the absorption is stable2About 50ppm.\|INVENTION MODE\|[0049] Example 8: CO 22The structure of the electrochemical capture and mineralization sealing system is the same as that of the embodiment 1, and the embodiment considers that the system is used for high-purity CO in the operation of high current density2Absorption effect of\|[0050] FIG. 8 shows the current density of 2A cm for the reaction module-2System for high purity CO2(99.995%) absorption over time. Here, the absorption rate is defined as CO2The ratio of the change in flow rate before and after entering the system to the inlet flow rate. The results show that the system has a relatively short settling time in this mode of operation, and that 13% absorption is achieved in the 3 minute system, with the absorption increasing with time and reaching a 15% absorption efficiency after 20 minutes.	(CN106757119)\|TECHNICAL FIELD\|[0002] The invention belongs to the technical field of capture and storage of carbon resources, and relates to a method for realizing CO2Electrochemical system for capture and mineralization sequestration\|BACKGROUND ART\|[0004] CO excessively discharged in China2Mainly from fossil fuel combustion, e.g. for power generation, but also from small dispersed sources, e.g. automobile engines, and combustion in residential and commercial buildingsA furnace; in addition to this, CO2Also in the refining of certain mineral resources. Currently, excessive emission of CO2Has led to an increasingly severe greenhouse effect, due to the large part of CO2Gas is absorbed by the ocean, which makes the ocean acidification problem increasingly serious. The concern of the international society on climate change leads to the emergence of the framework convention of climate change of the united nations, and further promotes CO2Development of capture and sequestration technology (CCS) technology.\|[0005] CCS technology generally includes three major components of capture, transport and containment. First, the capture step is to capture CO2Separated from other gaseous products. Such as combustion processes in power plants, separation techniques may be employed to capture CO after combustion2Or decarbonizing the fuel prior to combustion. Secondly, in order to capture CO2Transport to CO2The source is far away from the appropriate sequestration site, requiring transportation steps to be taken. Captured CO for ease of transportation and sequestration2High concentration compression is typically performed by the capture device. Last CO2The sequestration process is the core of CCS technology, determining the overall process cost and process complexity. Currently, CO2The sealing technology comprises three types of geological sealing, ocean sealing and mineralization sealing, and the technology is greatly different from the maturity of the market. Geological sequestration technology is relatively mature, and currently, industrial demonstration projects are available, such as: the Norwegian North sea Sleipner geological sequestration project has successfully injected 1000 million tons of CO into the ground2. However, the application area of geological sequestration is limited, which is not only closely related to the formation of geological rock, but also has high cost for later monitoring and maintenance, and is easy to cause geological disasters if leakage occurs.\|[0006] Ocean sequestration and mineralization sequestration are currently only in the research, development, or demonstration stages. Among these, the mineralization sequestration technology has great potential to develop, which mainly utilizes the basic or alkaline earth oxides, such as magnesium oxide and calcium oxide, present in naturally occurring silicate rocks to sequester CO2And (5) curing. These substances are mixed with CO2Chemical reactions produce compounds such as magnesium carbonate and calcium carbonate. The advantages of mineralization and sequestration are as follows: (1) wide raw material sourceAnd 4. preparing the compound. On the one hand, the reserves of silicate rock in the crust are enormous, while these oxides may also be present in certain industrial wastes, such as stainless steel slag and mineral ash; (2) CO 22After mineralization, the mineral is not released into the atmosphere, compared with geological storage and ocean storage, the mineral is free from subsequent monitoring and maintenance cost, and the storage risk is small; (3) the mineralized carbonate product has wide application, can be used as building materials and fireproof coatings, is also an important chemical raw material, and is widely applied to the industries of chemical industry, glass, paper making and the like.\|[0007] CO presently disclosed2There are two main types of capture and mineralization sequestration techniques. One is achieved by chemical methods, while the other is based on electrochemical methods. The former is mostly carried out at high temperature or high pressure, and the system structure is complex. For example, Olsen Espen discloses the use of metal oxide salt solutions to absorb CO at temperatures between 600 ℃ and 1600 ℃2The technology and process of (CN 102448581A, US 20120128559). Terasaka et al (chem. Eng. Technol.2006, 29No 9, pp. 1118-4) Absorption of CO as a working medium2The mineralization product is Li2CO3And Li2SiO3In the form of suspended solid particles. US2005036932 discloses an absorption and removal of CO from flue gas2By bubbling the exhaust gas through a stream containing CaO and/or Ca (OH)2Of solid particles of (a) so that CO in the exhaust gas is present2Conversion to CaCO3. CN 102491795A discloses CO at 150-350 deg.C2Under the condition that the partial pressure is not lower than 1.0MPa, the potassium feldspar is used for leading CO to be treated2A method for producing a potassium-rich solution by mineralization; CN 102895847A discloses that CO is introduced into2The trapping method comprises introducing molten alkali metal, alkaline earth metal, transition metal carbonate, silicate, borate, oxide, hydroxide, nitrate, aluminate and their mixture into the reactor for absorption electrolysis. CN 103111161A discloses a larger scale CO2Capture process by CO with positive pressure2Solvent capture of CO in a capture column2Supersaturated CO2The solution enters a releasing tower again for extraction and concentration.CO based electrochemical process2The capture and conversion process is relatively simple and the operating environment is relatively mild, CN 101670236A discloses recovery of CO by aqueous carbonate capture and electrodialysis2By aqueous solution capture of CO2Subsequent electrodialysis to form CO-rich2Liquid flow and regenerated capture solution. CN 102351310A discloses microbial electrochemical CO2A capture system using organic wastewater as a microbial nutrient source in CO2The problem of sewage treatment is considered while the sewage is captured. CN 102978653A discloses a mineralized CO2The membrane electrolysis method for coproducing strong acid is characterized by that its mineralized raw material is nitrate or sulfate, and its product is carbonate and nitric acid. CN 105420751 a discloses a method for preparing hydrocarbons by electrochemical reduction of carbon dioxide, which uses alkali metal carbonate (bicarbonate), sulfate, phosphate (bicarbonate), etc. as substances and electrolyte, and is characterized in that an organic solvent is introduced into an electrolyte system. Unlike electrochemical capture in aqueous systems, CN 103590064 a discloses the use of anhydrous LiF and Li2CO3The molar ratio (0.5-1.5): 1, uniformly mixing, adding an additive to prepare electrolyte molten salt, placing the electrolyte molten salt in an electrolytic cell, heating to 690-700 ℃, and introducing CO2An electrolytic capture method. Wherein the cathode material is Ni or Ti, and the anode material is Pt, Fe-Ni alloy or Fe-Ni-Al2O3And (3) alloying.\|DISCLOSURE\|[0008] Disclosure of Invention\|[0009] In order to overcome the defects in the prior art, the invention provides a method for realizing CO2An electrochemical system for capturing, mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed; the liquid flow discharged after the system is operated is alkaline, and the treatment of ocean acidification problems in a designated area can be realized to a certain extent.\|[0010] Can realize CO2The technical scheme of the electrochemical system for capturing, mineralizing and sealing up comprises the following steps:\|[0011] the system comprises a fluid power module, a reaction module and a control and display module, wherein the fluid power module is connected with the reaction module and provides CO for the reaction module2The feed gas and the supplementary electrolyte and the reactant of (1); the reaction module is CO2The capture and mineralization sealing provides a reaction site, which comprises an anode chamber, a cathode chamber and a diaphragm; the anode chamber is internally provided with an electrode, electrolyte, silicate and/or mineral containing silicate, and the cathode chamber is internally provided with an electrode and electrolyte; the anode chamber is separated from the cathode chamber by a diaphragm; the control and display module is simultaneously connected with the reaction module and the fluid power module, provides running electric power for the fluid power module, and simultaneously realizes a steady state or transient state and steady state combined electrochemical reaction mode for the reaction module, so that silicate is converted into carbonate, and CO is realized2Capture and mineralize and seal up.\|[0012] The diaphragm in the reaction module comprises an anion-exchange membrane, a cation-exchange membrane or a microporous membrane (such as a porous polytetrafluoroethylene membrane); the electrode material comprises simple substances, alloys or compounds formed by other nonmetal elements containing Pt, Re, Pd, Rh, Mo, Wo, Nb, Ru, Ir, Sn, Mn, Fe, Co, Ni, Cu, Ag and C. The silicate includes all compounds or mixtures containing silicon, oxygen and other chemical elements (such as aluminum, iron, calcium, magnesium, manganese, potassium, sodium, barium, copper, zinc, lead, tin). The silicate-containing mineral includes olivine, serpentine, basalt, asbestos, mica, talc, kaolinite, montmorillonite, zeolite, agalmatolite, tourmaline, pyroxene, and hornblende containing the above silicate components.\|[0013] The anode is of a flat electrode structure or a porous electrode structure.\|[0014] CO treated in the anode chamber2The concentration range of the mixed gas is between 0.050% and 99.995%.\|[0015] When the operation mode of the reaction module is steady state, the working current density range is 0.075mA/cm2～2 A/cm2To (c) to (d); when the operation mode of the reaction module is transient, a sine wave, a square wave and a three wave of current or voltage are loaded on the systemThe angular wave signal has a variation frequency range of 1000 Hz-0.1 Hz.\|[0016] The control and display module comprises a sensing device, a system control device and a display device; wherein the sensing device comprises H2、O2、CO2A concentration sensor, a temperature sensor, a liquid level sensor and a pressure sensor; the display device is used for displaying temperature, pressure and O in system operation2Concentration, H2Concentration, CO2Concentration, level, current, voltage information; on one hand, the system control device provides electric power for the sensing device and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a digital signal processor in the system control device controls the operation of the reactor, and provides a steady-state operation mode, a transient-state operation mode or a steady-state and transient-state combined operation mode for the system.\|[0017] CO of system treatment2The concentration range of the gas is wide, namely high-concentration CO can be realized2(99.99%) conversion can also be used for trace amounts of CO in air2(ppm level) conversion, System CO2The transformation scale of (2) is controllable and modularization is easy to realize. The discharged product of the system after operation is environment-friendly and alkaline, and the system can realize CO2The problem of ocean acidification which is becoming more serious at present can be simultaneously relieved while the capture and the mineralization are sealed.\|[0018] The invention realizes CO by adopting an electrochemical method2Compared with the application of physical methods (including geological storage and ocean storage), the technology does not need to be monitored in the later period and has no risk of geological disasters. Compared with the existing applied chemical method to realize CO2Compared with the technology of capture and mineralization sealing, the invention applies the electrochemical method without high temperature and high pressure reaction environment, the reaction can be carried out at normal temperature and normal pressure, the system has simple structure and low energy consumption, and is easy to realize modular design and has huge application prospect.\|DRAWINGS DESCRIPTION\|[0020] FIG. 1 is CO2The structure of the electrochemical capture and mineralization sealing system is shown schematically.\|[0021] FIG. 2 is introduction of calcium silicate to CO in air2The absorption efficiency and the system cell pressure.\|[0022] FIG. 3 is a graph of silicate species vs. CO in the air of the system2The effect of the absorption effect of (c).\|[0023] FIG. 4 is a graph of the system versus CO in air at different current densities2The absorption effect of (1).\|[0024] Wherein (a) is CO2A time-dependent profile; (b) after 3 hours, CO2Concentration profile with system power.\|[0025] FIG. 5 shows 4mA cm of electrode material at room temperature for a system-2For CO in air under the condition2The effect of absorption.\|[0026] Wherein (a) is CO2The change in concentration over time; (b) is the change of the system tank pressure with time.\|[0027] FIG. 6 shows the system operating under unsteady state current conditions for CO in air2The absorption effect of (1).\|[0028] Wherein (a) is the variation of the system current with time; (b) is CO2The change in concentration with time.\|[0029] FIG. 7 is a graph of the system versus CO in air at low current density2The absorption effect of (1).\|[0030] FIG. 8 is a graph of system for high purity CO at high current density2The absorption effect of (1).\|INVENTION MODE\|[0031] Detailed Description\|[0032] To further illustrate the invention, the following examples are presented to describe CO2The electrochemical capture and containment system is not intended to limit the scope of the invention.\|INVENTION MODE\|[0033] Example 1: CO 22Electrochemical capture and containment system architecture\|[0034] FIG. 1 shows CO2And (3) an electrochemical capture and mineralization sequestration system structure. The system consists of a fluid power module, a reaction module and a control and display module. The fluid power module is connected with the reaction module and can be provided with CO2May also be supplemented with supporting electrolytes and reactants. The control and display module is simultaneously connected with the reaction module and the fluid power module, and the system controller provides electric power for the sensing device on one hand and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a Digital Signal Processor (DSP) in the controller can control the operation of the reactor, provide steady-state, transient-state, steady-state and transient-state combined operation modes for the system and realize shutdown operation. The reaction module is the core component of the system and is CO2The capture and mineralization sealing provides a reaction site, and the structure of the device consists of an anode chamber, a cathode chamber and a diaphragm. The anode chamber and the cathode chamber are respectively provided with an anode, an anolyte, a cathode and a catholyte, wherein the anode chamber contains silicate.\|INVENTION MODE\|[0035] Example 2: CO 22The electrochemical capture and mineralization sequestration system is the same as example 1, which compares the addition or non-addition of silicate to the system CO2Absorption efficiency and emission of products.\|[0036] FIG. 2 shows electrochemical CO with and without silicate minerals2A capture and mineralization sealing system with a current density of 2mA cm-2Under the condition, the system can be used for treating CO in the air2The absorption effect and the system tank pressure. It can be seen that the introduction of calcium silicate is for CO2The absorption and system power consumption effects of (1) produced significant results after 100 minutes, calcium silicate containing system exhaust gas CO2The concentration is relatively low. Table 1 shows the effect of silicate incorporation on the pH of the effluent after 8 hours of operation of the system, which is seen in calcium silicate incorporationThe acidification degree of the anode discharge product is obviously reduced.\|[0037] TABLE 1 Effect of silicate incorporation on the pH of the anode and cathode compartments\|[0038] \|INVENTION MODE\|[0039] Example 3: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, in this example, silicate species are compared to system CO2The absorption efficiency of (a).\|[0040] FIG. 3 shows the reaction at CO2After calcium silicate, magnesium silicate, aluminum silicate and sodium silicate are introduced into the electrochemical capture and mineralization sealing system, the system can be used for treating CO in the air at room temperature2Comparison of absorption effects. The reaction module is operated in a steady-state constant current mode in the system operation, and the current is 2 mA-cm-2. It can be seen that the type of silicate affects the system CO2Transient and steady state behavior of the absorption. System Pair CO introducing aluminum silicate and magnesium silicate 1 hour after system startup2The absorption effect is inferior to that of the system containing calcium silicate and sodium silicate. After 3 hours of operation, the system had entered steady state, with systems employing magnesium silicate for CO2The absorption effect of (A) is inferior to that of the other three silicates.\|INVENTION MODE\|[0041] Example 4: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, this example considers the current density to the system CO2The effect of the absorption effect.\|[0042] Experiment researches electrochemical CO2The capture and mineralization sealing system has different current densities of 0.5 mA-cm-2～6mA·cm-2For CO in air when silicate A is contained2The absorption effect of (2) is shown in FIG. 4 (a). It can be seen that as the current density increases, the mixed gas is dischargedCO2Reduced content, system to CO2The time for absorption to reach stability increases. However, the system is for CO in air2Is not proportional to the output of system power, and fig. 4(b) shows CO in the system exhaust2The concentration of (A) is varied with the system power and is 0.5mA cm-2～6mA·cm-2In the current density range, CO2The increase in processing power of (a) is accompanied by an exponential increase in system power.\|INVENTION MODE\|[0043] Example 5: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, this example compares the electrode material to the system CO2The effect of the absorption effect.\|[0044] FIG. 5(a) shows the CO content of the system in air when the anode electrode materials are copper sheet, platinum sheet, foam copper and foam nickel respectively2And (5) comparing the absorption effect. Wherein, the copper sheet and the platinum sheet are flat electrodes, and the foam copper and the foam nickel are porous electrodes. It can be seen that under the premise of the same current density, the change of the electrode material can be used for CO in the air2The absorption effect of (2) has an influence, and the system tank pressure changes remarkably. When the foam nickel with the porous structure is used as the anode, the power consumption is minimum, and the energy is saved most.\|INVENTION MODE\|[0045] Example 6: CO 22The structure of the electrochemical capture and mineralization sequestration system is the same as that of the embodiment 1, and the reaction module in the embodiment operates in a transient state and steady state combined operation mode.\|[0046] FIG. 6 shows the system pairs and CO in air for the transient and steady state combined operation mode of the reaction module2Wherein the area of the electrode used for the anode in the reaction module is 4cm2. FIG. 6(a) shows the change of the current of the reaction module with time, the system is at 6mA (1.5mA cm) in 0-5 min-2) On the basis, 2mA (0.5mA cm) is loaded-2) The frequency of the current change is 1 Hz; changing the frequency of the loading alternating current signal to 0.1Hz in the following 25 minutes; in thatThe frequency change is increased to 1000Hz in 30-55 minutes, and in the last 25 minutes, the system is in an intermittent discharge mode, namely, the system stops for 1 minute every 5 minutes of operation. FIG. 6(b) shows the system outlet CO in the operating mode as shown in FIG. 6(a)2The concentration of (c) is varied. It can be seen that in the transient and steady state combined operation mode, the system still works against CO in air2Has obvious effect on absorption.\|INVENTION MODE\|[0047] Example 7: CO 22The structure of the electrochemical capture and mineralization sequestration system is the same as that of the embodiment 1, and the embodiment considers that the system is used for CO in the air when the current is low2Absorption effect of\|[0048] FIG. 7 shows the use of 0.075mA cm in the reaction module-2System for CO in air2The absorption effect of (1). The results show that the system is in this mode of operation, after 20 minutes, towards CO2The absorption enters a stable operation state, and the CO in the air can be reduced after the absorption is stable2About 50ppm.\|INVENTION MODE\|[0049] Example 8: CO 22The structure of the electrochemical capture and mineralization sealing system is the same as that of the embodiment 1, and the embodiment considers that the system is used for high-purity CO in the operation of high current density2Absorption effect of\|[0050] FIG. 8 shows the current density of 2A cm for the reaction module-2System for high purity CO2(99.995%) absorption over time. Here, the absorption rate is defined as CO2The ratio of the change in flow rate before and after entering the system to the inlet flow rate. The results show that the system has a relatively short settling time in this mode of operation, and that 13% absorption is achieved in the 3 minute system, with the absorption increasing with time and reaching a 15% absorption efficiency after 20 minutes.	Family Number\|(76279049)\|76279049\|Object of Invention\|(CN106757119B B)\|In order to overcome the defects in the prior art , the invention provides a method for realizing CO2An electrochemical system for capturing , mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed ; the liquid flow discharged after the system is operated is alkaline , and the ( . . . ) \|(CN106757119 A)\|In order to overcome the defects in the prior art , the invention provides a method for realizing CO2An electrochemical system for capturing , mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed ; the liquid flow discharged after the system is operated is alkaline , and the ( . . . ) \|Abstract\|(CN106757119B B)\|The invention belongs to the technical field of carbon resource capturing and storing and relates to a system for achieving CO2 capturing and mineralization through an electrochemical method . The system is structurally composed of three parts of a hydrodynamic force module , a reaction module and a control and display module . By means of the electrochemical technology of a steady state , a transient state and combination of the steady state and the transient state , silicate is converted into carbonate , and CO2 capturing and mineralization are achieved . The CO2 capturing and mineralization system is mainly used for relieving the increasing greenhouse effect , liquid flow drained by the system is alkaline , and treatment of ocean acidification of local areas is achieved at the same time . The system can also be used for adjusting the concentration of CO2 gas in a closed space in real time and can also serve as an auxiliary facility for emission reduction of large CO2 emission enterprises . \|	Surface technology, coating	C25B-001/00\|C25B-015/02\|Y02C-020/40		C25B-001/00\|C25B-015/02\|Y02C-020/40	C25B-001/00\|C25B-015/02	C25B-001/00\|C25B-015/02			CN109855206\|CN117023729B\|CN117233253B	CN109855206 84771358 WHO=Examiner SELF=N CAT=A\|CN117023729B 107214603 WHO=Examiner SELF=N\|CN117233253B 107757227 WHO=Examiner SELF=N	CN102899679\|CN101134155\|KR20160119429\|CN104477950\|CN103966622\|US20140238871\|US9464010\|CN103230735\|CN103173782\|CN102978653\|CN102895847\|CN102762277\|CN101878060\|JP2010125354	CN102899679 8151397 WHO=Examiner SELF=N CAT=Y\|CN101134155 6409477 WHO=Examiner SELF=N CAT=Y\|KR20160119429 74446448 WHO=Examiner SELF=N CAT=A\|CN104477950 68955167 WHO=Examiner SELF=N CAT=A\|CN103966622 67167903 WHO=Examiner SELF=N CAT=A\|US20140238871 1895012 WHO=Examiner SELF=N CAT=A\|US9464010 65403965 WHO=Examiner SELF=N CAT=A\|CN103230735 45750692 WHO=Examiner SELF=N CAT=A\|CN103173782 45517523 WHO=Examiner SELF=N CAT=A\|CN102978653 8171552 WHO=Examiner SELF=N CAT=A\|CN102895847 8135679 WHO=Examiner SELF=N CAT=A\|CN102762277 1910468 WHO=Examiner SELF=N CAT=A\|CN101878060 6949869 WHO=Examiner SELF=N CAT=A\|JP2010125354 33126904 WHO=Examiner SELF=N CAT=A	理查德•A•斯科特等: "《防护用纺织品》", 31 March 2016, 中国纺织出版社 (Cat. A)	CN101134155; CN103966622; CN103230735; CN101878060; CN102762277; CN103173782; CN102895847; CN102978653; CN104477950; US20140238871; JP2010125354; KR20160119429; US9464010; CN102899679		GRANTED	(CN106757119)\|GRANTED	ALIVE	(CN106757119)\|ALIVE	(CN106757119)\|LEGAL DETAILS FOR CN106757119\|Actual or expected expiration date=2036-12-09\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2016-12-09\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201611128528\|Application date=2016-12-09\|Standardized application number=2016CN-1128528\|Event publication date=2017-05-31\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN106757119\|Publication stage code=A\|Publication date=2017-05-31\|Standardized publication number=CN106757119\|Event publication date=2017-05-31\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2017-06-23\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2019-02-26\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN106757119\|Publication stage code=B\|Publication date=2019-02-26\|Standardized publication number=CN106757119B\|Event publication date=2019-02-26\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right		(CN106757119)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjn+frZymVg1jxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000022549569&ekey=1953&xpn=CN106757119B&kind=B	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=kWAwQSdm5YD2iOc1MipqmrmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN106757119)\|CN\|(CN106757119)\|CN	(CN106757119)\|NAME=DALIAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN\|(CN106757119)\|NAME=DALIAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN		(CN106757119)\|NAME=MEI HONGYU;PATENT AGENCY CENTER OF DLUT , REG=21200\|(CN106757119)\|NAME=MEI HONGYU;PATENT AGENCY CENTER OF DLUT , REG=21200		(CN106757119)\|NAME=MAO QING\|NAME=CUI JIANMING\|NAME=HUANG YANQIANG\|NAME=LIU JIANJUN\|NAME=JING WEIYUN\|NAME=SHI YUE\|(CN106757119)\|NAME=MAO QING\|NAME=CUI JIANMING\|NAME=HUANG YANQIANG\|NAME=LIU JIANJUN\|NAME=JING WEIYUN\|NAME=SHI YUE	(CN106757119)\|8	1	1					(CN106757119)\|Gazette date: GAZDATE=2019-02-26\|Gazette number: GAZNUM=35-0901\|Number of Pages: NPAGES=13\|Primary examiner: 刘燕\|Primary examiner: Liu Yan\|\|(CN106757119)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2017-05-31\|Gazette number: GAZNUM=33-2201\|Number of Pages: NPAGES=13\|Primary examiner: 刘燕\|Primary examiner: Liu Yan\|		(CN106757119)\|CHINESE (CHI)	(CN106757119B)\|Patent\|(CN106757119)\|Patent	Titre: (CN106757119)\|One kind is for realizing CO2The electro-chemical systems that capture is sealed up for safekeeping with mineralising Résumé: (CN106757119)\|The invention belongs to the technical field of carbon resource capturing and storing and relates to a system for achieving CO2 capturing and mineralization through an electrochemical method. The system is structurally composed of three parts of a hydrodynamic force module, a reaction module and a control and display module. By means of the electrochemical technology of a steady state, a transient state and combination of the steady state and the transient state, silicate is converted into carbonate, and CO2 capturing and mineralization are achieved. The CO2 capturing and mineralization system is mainly used for relieving the increasing greenhouse effect, liquid flow drained by the system is alkaline, and treatment of ocean acidification of local areas is achieved at the same time. The system can also be used for adjusting the concentration of CO2 gas in a closed space in real time and can also serve as an auxiliary facility for emission reduction of large CO2 emission enterprises.	28	Abstract	gpt-4o-mini	yes	The article describes a system that uses electrochemical methods to capture CO2 and convert silicates into carbonates, which aligns with the topic of enhanced weathering and carbon sequestration.
31	CN202410297703	CN202410297703	CN118189424	110191082	CN118189424 A 2024-06-14 [CN118189424]	2024-03-15	2024-03-15	2024-06-14		(CN118189424)\|2044-03-15	(CN118189424)\|Method for generating terrestrial heat and extracting valuable elements by permanently sealing carbon dioxide through geological rock under assistance of ammonium bisulfate	(CN118189424)\|The invention discloses a method for generating terrestrial heat and extracting valuable elements by permanently sealing and storing carbon dioxide through geological rocks under the assistance of ammonium bisulfate. The method comprises the following steps that under the assistance of ammonium bisulfate, silicate rock minerals containing magnesium, calcium and iron in a geologic structure react with injected carbon dioxide, carbon dioxide is permanently sealed, meanwhile, terrestrial heat is generated, and valuable elements rich in leachate silicate are recycled. According to the method, under the assistance of ammonium bisulfate, injected carbon dioxide mixed liquid reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is rapidly generated, the mineralization fixing process is fast, meanwhile, heat release and the reaction rate are coupled to improve the geothermal grade, the reaction is accelerated through ammonium bisulfate, the mineralization reaction rate is increased, and the mineralization effect is improved. The heat release process of the mineral carbonization reaction is coupled with the reaction rate to improve the geothermal grade.	GUANGZHOU INSTITUTE OF ENERGY CONVERSION - CHINESE ACADEMY OF SCIENCES	(CN118189424)\|GUANGZHOU INSTITUTE OF ENERGY CONVERSION CHINESE ACADEMY OF SCIENCES ([CN])	CAO YAN	(CN118189424)\|CAO YAN	(CN118189424)\|FANG YAN;GUANGZHOU KEYUE I.P. LAW OFFICE\|Reg. Nb: 44001\|MO YAOJIANG;GUANGZHOU KEYUE I.P. LAW OFFICE\|Reg. Nb: 44001	(CN118189424)\|Compared with the prior art, the invention has the following advantages:\|The invention applied by the inventor realizes permanent fixation by utilizing the reaction of silicate minerals rich in magnesium, calcium and iron in geological strata and CO 2, but the risk of leakage of CO 2 back to the atmosphere can be greatly reduced and heat release is also accompanied; however, this process is very slow, and it is difficult and long time to accumulate valuable heat energy for use under the heat dissipation conditions of the geological structure, and the geological sequestration depth of CO 2 is generally better in the range of 2000-3000 meters, and this depth brings about thresholds such as drilling cost, compression energy consumption of CO 2, and the like.\|	(CN118189424)\|1. A method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which is characterized by comprising the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid.\|	(CN118189424)\|Aiming at the problems existing in the prior art, the invention provides a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide assisted by ammonium bisulfate, which can obviously accelerate the carbonization reaction path of minerals in stratum, accelerate heat release by faster reaction, drive considerable temperature rise of the rock and improve geothermal grade and economic benefit feasibility of heat collection. The invention aims to provide a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which comprises the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid. The invention discloses a carbonization reaction path capable of remarkably accelerating minerals in a stratum, accelerating heat release by faster reaction, driving considerable temperature rise of rock, and improving geothermal grade and economic benefit feasibility of heat collection.\|The invention discloses a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate.\|The invention relates to the technical field of carbon dioxide sequestration, in particular to a method for generating geothermal heat and extracting valuable elements by permanently sequestering carbon dioxide by using geological rock with the aid of ammonium bisulfate.\|	(CN118189424)\|CARBON DIOXIDE(100,41)\|AMMONIUM BISULFATE(100,38)\|GEOLOGICAL ROCK(100,12)\|GEOTHERMAL HEAT GENERATION(100,9)\|SEAL CARBON DIOXIDE(100,4)\|STORE CARBON DIOXIDE(100,1)\|GEOTHERMAL GRADE(74,17)\|ECONOMIC BENEFIT FEASIBILITY(69,2)\|GEOLOGICAL SEQUESTRATION DEPTH(61,1)\|AMMONIUM BISULFATE ASSISTANCE(59,9)\|LEACHING LIQUID(41,3)\|MINERAL ACCELERATION(38,1)\|SILICATE MINERAL(37,12)\|CARBONIZATION REACTION PATH(37,2)\|SILICATE GEOLOGICAL MINERAL(35,4)\|MINERAL CARBONIZATION REACTION PATH(31,1)\|GEOLOGY INDIRECT CARBONIZATION(30,8)\|FAST REACTION(29,2)\|PERMANENT FIXATION(29,2)\|SILICATE(28,6)\|AMMONIUM BISULFATE AID(28,1)\|GEOLOGICAL STRUCTURE(27,7)\|HEAT COLLECTING(27,2)\|STRATUM PERMEABILITY(25,4)\|STRATUM POROSITY(25,4)\|STRATUM(24,3)\|ACCELERATING HEAT(23,1)\|GEOTHERMAL HEAT(20,5)\|STRATUM MINERAL VOLUME(19,4)\|CARBON DIOXIDE SEQUESTRATION(19,3)\|UNDERGROUND DEPTH(18,5)\|GEOLOGICAL STRATA(18,2)\|TEMPERATURE GEOTHERMAL GRADE(18,2)\|COBALT RICH(17,4)\|DRILLING COST(17,2)\|SEQUESTERING CARBON DIOXIDE(17,1)\|GEOLOGICAL MINERAL CARBONIZATION(15,2)\|COMPRESSION ENERGY CONSUMPTION(13,2)\|WOLLASTONITE(13,2)\|VALUABLE HEAT ENERGY(13,1)\|FLUID MIXING(12,7)\|ANORTHITE(12,2)\|SEEPAGE(11,6)\|STRATUM TEMPERATURE(11,4)\|BASALT(11,2)\|HEAT DISSIPATION(11,1)\|GEOLOGY DIRECT CARBONIZATION(10,3)\|MINERALIZATION REACTION RATE(9,4)\|SEALING CARBON DIOXIDE(9,2)\|FORMATION CONDITION(8,4)\|ENERGY CONSUMPTION(8,2)\|GEOLOGICALLY DIRECT CARBONIZATION(8,2)\|MEDIUM TEMPERATURE(8,2)\|ASSISTED PERMANENT SEQUESTRATION(8,1)\|GEOLOGICAL INDIRECT CARBONIZATION FEATURE(8,1)\|OLIVINE MAGNESIUM EXTRACTION EXPERIMENT(8,1)\|TEMPERATURE RISE(7,9)\|STRATUM FLOW PRESSURE(7,4)\|ANNUAL CARBON SEQUESTRATION(7,3)\|OLIVINE SAMPLE(7,3)\|SHALLOW OLIVINE(7,2)\|SIMULTANEOUSLY COUPLING HEAT RELEASE(7,2)\|ELECTRON MICROSCOPIC CRACK GRAPH(7,1)\|GEOLOGICAL SEQUESTRATION(7,1)\|STRATUM CONDITION(6,4)\|CHINA ECONOMIC BENEFIT(6,1)\|GEOLOGICAL ROCK STRATUM(6,1)\|OLIVINE FLAKE(6,1)\|OLIVINE TON(6,1)\|SEALING GEOLOGICAL GRADE(6,1)\|CARBON DIOXIDE MIXED SOLUTION(5,4)\|DRILLING SEALING(5,2)\|LEACHING SOLUTION IRON SILICATE(5,2)\|RECYCLING POTENTIAL(5,2)\|UNTREATED SAMPLE(5,2)\|CARBONATION CAPACITY(5,1)\|CHRYSOTILE MG(5,1)\|COBALT PRODUCTIVITY(5,1)\|DIFFICULT TIME(5,1)\|ELEMENTAL SCAN SPECTRUM(5,1)\|EXTRACTABLE NICKEL(5,1)\|MAGNESIUM CALCIUM SILICATE ROCK(5,1)\|MAGNESIUM ELEMENTAL DISTRIBUTION(5,1)\|MINERAL CARBONIZATION MODE(5,1)\|OLIVINE MINERAL(5,1)\|SEALING GEOLOGICAL DEPTH(5,1)\|TREND ASCENSION(5,1)\|AVERAGE OLIVINE TEMPERATURE RISE(4,7)\|CARBON DIOXIDE PRESSURE(4,6)\|MASS TRANSFER(4,6)\|REACTION MATURATION TIME(4,6)\|INJECTION CONDITION(4,4)\|BOX BENHNKEN(4,1)\|COBALT NICKEL EXTRACTION(4,1)\|CORE SEM CRACK DIAGRAM(4,1)\|CORE SLICE(4,1)\|DEVELOPMENT RESOURCE(4,1)\|GEOLOGICAL SEALING(4,1)\|GEOLOGICALLY INDIRECT CARBONIZATION RESULT(4,1)\|GEOTHERMAL ENERGY BENEFIT(4,1)\|LOGARITHMIC RELATIONSHIP(4,1)\|OLIVE STRATA TEMPERATURE(4,1)\|OLIVINE MG(4,1)\|SMELTING BENEFIT(4,1)\|SQUARE KILOMETER FOREST(4,1)\|STEAM COLLECTION(4,1)\|REACTION TEMPERATURE(3,4)\|BRUCITE(3,2)\|IRON CONTENT(3,2)\|SEM TEST(3,2)\|STABLE CARBONATE(3,2)\|WEAK ALKALI SALT(3,2)\|ANNUAL CARBON STORAGE(3,1)\|BRINE LAYER DEPTH(3,1)\|CARBON NEUTRALIZATION(3,1)\|COBALT CAPACITY(3,1)\|CRACK DEPTH(3,1)\|DRY HOT ROCK(3,1)\|EXPERIMENTAL FACTOR(3,1)\|EXTRACTING MG(3,1)\|FACTOR INTERACTION(3,1)\|FORMATION PERMEABILITY(3,1)\|FORMATION POROSITY(3,1)\|GEOLOGICAL DIRECT CARBONIZATION TEMPERATURE(3,1)\|GEOLOGICAL STORAGE(3,1)\|GEOLOGY INDIRECT CARBONIZATION RESULT(3,1)\|KG YEAR(3,1)\|PRESSURIZED INJECTION(3,1)\|REACTION ACCELERATOR(3,1)\|REACTION PROGRESSION(3,1)\|RECOVERING NICKEL(3,1)\|ROCK SAMPLE(3,1)\|SILICATE MINERAL PROPOSITION(3,1)\|	(CN118189424)\|1. A method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which is characterized by comprising the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid.\|2. The method according to claim 1, characterized in that it comprises in particular the following steps: injecting a mixed fluid of ammonium bisulfate and carbon dioxide into a stratum of silicate minerals containing magnesium, calcium and iron, reacting the mixed fluid with the silicate minerals containing magnesium, calcium and iron to generate carbonate, permanently sealing carbon dioxide, simultaneously coupling heat release and reaction rate to improve geothermal grade, and recovering valuable elements nickel and cobalt rich in silicate in the leaching solution.\|3. The method of claim 2, wherein the formation conditions comprise: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3.\|4. The method of claim 2, wherein the injection conditions of the mixed fluid of ammonium bisulfate and carbon dioxide comprise: the temperature of the mixed fluid is 20-200 ℃, the pressure of carbon dioxide is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection.\|5. The method of claim 2, wherein the geothermal grade is a medium and high temperature geothermal grade greater than 150 ℃.\|6. A method according to claim 1 or 2, wherein the silicate minerals comprise olivine, serpentine, basalt, wollastonite and anorthite which are rich in magnesium, calcium and iron.\|7. The method according to claim 1 or 2, wherein the concentration of NH 4HSO4 in the mixed fluid is 0.1-2.0mol/L and the solid-to-liquid ratio of silicate mineral to NH 4HSO4 solution is 100-1000kg/L.\|8. Use of the method of claim 1 or 2 for sequestering carbon dioxide.	(CN118189424)\|TECHNICAL FIELD\|[0001] The invention relates to the technical field of carbon dioxide sequestration, in particular to a method for generating geothermal heat and extracting valuable elements by permanently sequestering carbon dioxide by using geological rock with the aid of ammonium bisulfate. \|BACKGROUND ART\|The background technology is as follows:\|[0002] large scale carbon capture, utilization and sequestration (CCUS) technologies must be developed to achieve carbon neutralization, which involves injection of CO 2 into geological structures, such as deep brine layers or Enhanced Oil Recovery (EOR) in oil fields, but may involve leakage of freely stored CO 2 back to the atmosphere. \|[0003] The invention applied by the inventor realizes permanent fixation by utilizing the reaction of silicate minerals rich in magnesium, calcium and iron in geological strata and CO 2, but the risk of leakage of CO 2 back to the atmosphere can be greatly reduced and heat release is also accompanied; however, this process is very slow, and it is difficult and long time to accumulate valuable heat energy for use under the heat dissipation conditions of the geological structure, and the geological sequestration depth of CO 2 is generally better in the range of 2000-3000 meters, and this depth brings about thresholds such as drilling cost, compression energy consumption of CO 2, and the like.\|[0004] In view of the fact that geothermal energy has become one of the most competitive renewable energy utilization modes, the CO 2 geological sequestration is indeed capable of generating geothermal-like heat for utilization, and a new method is needed to achieve carbon dioxide sequestration while improving geothermal grade.\|DISCLOSURE\|The invention comprises the following steps:\|[0005] Aiming at the problems existing in the prior art, the invention provides a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide assisted by ammonium bisulfate, which can obviously accelerate the carbonization reaction path of minerals in stratum, accelerate heat release by faster reaction, drive considerable temperature rise of the rock and improve geothermal grade and economic benefit feasibility of heat collection. \|[0006] The invention aims to provide a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which comprises the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid.\|[0007] The invention discloses a carbonization reaction path capable of remarkably accelerating minerals in a stratum, accelerating heat release by faster reaction, driving considerable temperature rise of rock, and improving geothermal grade and economic benefit feasibility of heat collection. According to the invention, strong acid weak alkali salt (ammonium bisulfate NH 4HSO4) is adopted to accelerate the reaction of magnesium calcium silicate in a geological structure and injected CO 2, NH 4HSO4 has the potential of recycling, nickel and cobalt high-value elements rich in magnesium, calcium and iron silicate in leaching liquid are recovered, the nickel and cobalt productivity is improved to meet the requirements of clean energy sources of electric automobiles, the carbon footprint in mining activities is reduced, and high-purity amorphous silicon dioxide and brucite produced by subsequent processing of the solution can also be used for other chemical production.\|[0008] The method provided by the invention is characterized in that under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade.\|[0009] Preferably, the method specifically comprises the following steps: injecting a mixed fluid of ammonium bisulfate and carbon dioxide into a stratum of silicate minerals containing magnesium, calcium and iron, reacting the mixed fluid with the silicate minerals containing magnesium, calcium and iron to generate carbonate, permanently sealing carbon dioxide, simultaneously coupling heat release and reaction rate to improve geothermal grade, and recovering valuable elements nickel and cobalt rich in silicate in the leaching solution.\|[0010] The method provided by the invention is to inject the mixed fluid of CO 2 and ammonium bisulfate into a well, seal the well, open the well after the reaction is mature, collect steam and nickel-cobalt solution, realize that geological rock permanently seals carbon dioxide to generate geothermal heat and extract valuable elements nickel-cobalt.\|[0011] The invention continuously pushes the proposed silicate minerals which are rich in magnesium, calcium and iron in geological strata to react with CO 2 to realize permanent fixation technology, adopts strong acid weak alkali salt (such as ammonium bisulfate NH 4HSO4), accelerates the reaction of magnesium calcium silicate rock in geological structures with injected CO 2, and NH 4HSO4 has recoverable recycling potential, simultaneously recovers nickel and cobalt high-value elements which are rich in magnesium, calcium and iron silicate in leaching solution, improves the nickel and cobalt capacity to meet the requirements of clean energy of electric vehicles, reduces the carbon footprint in mining activities, ensures that the high-purity amorphous silicon dioxide and brucite which are produced by subsequent processing of the solution can also be used for other chemical production, changes the defect of very slow conventional permanent sealing reaction rate, improves the sealing geological grade, simultaneously reduces the sealing geological depth, and obtains high-value elements including recovered nickel and cobalt, reduces the cost, the compression energy consumption of CO 2 and the like.\|[0012] Preferably, the formation conditions include: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3. Different injection conditions and stratum conditions bring different geological mineral carbonization effects, and corresponding injection conditions are selected under different stratum conditions, so that the energy utilization rate is improved. Further preferably, the formation conditions include: the underground depth is 1000-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3.\|[0013] Preferably, the injection conditions of the mixed fluid of ammonium bisulfate and carbon dioxide comprise: the temperature of the mixed fluid is 20-200 ℃, the pressure of carbon dioxide is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection.\|[0014] Preferably, the geothermal grade is a medium and high temperature geothermal grade greater than 150 ℃.\|[0015] Preferably, the silicate minerals include olivine, serpentine, basalt, wollastonite and anorthite which are rich in magnesium, calcium and iron.\|[0016] Preferably, the concentration of NH 4HSO4 in the mixed fluid is 0.1-2.0mol/L, the solid-to-liquid ratio of silicate mineral to NH 4HSO4 solution is 100-1000kg/L, and the reaction temperature is 50-180 ℃.\|[0017] The invention also protects the application of the method in carbon dioxide sequestration.\|[0018] Compared with the prior art, the invention has the following advantages:\|[0019] 1. According to the method provided by the invention, in the geological rock and 2-year period, the initial temperature of the related geological rock stratum and the temperature of the CO 2 fluid injected are 37 ℃ and 1 cubic kilometer, the average temperature rise of the rock can reach 105 ℃ and reach 142 ℃ at the final temperature, high geothermal grade reaction heat is generated, and meanwhile, the geological storage CO 2 amount can reach 11.9 ten thousand tons each year, which is equivalent to the annual carbon storage amount of 342k square kilometer forests in northwest China; if the temperature of the fluid injected with CO 2 and the initial rock temperature are further increased to 90 ℃, the rock temperature rise and the average CO 2 sealing rate are increased by more than 60% compared with those at 37 ℃, the rock temperature after 2 years is increased by 181 ℃, and the grade of the high-temperature geothermal grade is far more than 150 ℃. Meanwhile, the extraction efficiency of valuable elements nickel and cobalt exceeds 50%, the total CO 2 sealing benefit, geothermal benefit and valuable element mining and smelting benefit are obtained, and each sealing 1 ton of CO 2 can obtain remarkable economic benefit, so that the high cost situation of CO 2 geological sealing is thoroughly twisted. \|[0020] 2. The method provided by the invention is characterized in that under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade.\|DRAWINGS DESCRIPTION\|Description of the drawings:\|[0021] FIG. 1 is a schematic view of a geological vertical section of the invention with ammonium bisulfate assisted permanent sequestration of CO 2 while producing geothermal heat and extracting valuable elements. \|[0022] Fig. 2 is an X-ray diffraction spectrum of the sample of olivine of example 1.\|[0023] FIG. 3 is an electron microscopy image (a) and elemental scan spectra (b-d) of the olivine flakes of example 1.\|[0024] FIG. 4 is a plot of response surface and contour of the two-factor interaction versus magnesium response rate in example 2.\|[0025] FIG. 5 is a graph showing the surface reaction rate of the olivine with NH 4HSO4 as a function of (a) NH 4HSO4 and (b) 1/T in example 3.\|[0026] FIG. 6 is a graph of the K-penetration (c) after the treatment of the olivine, showing the results (a) of the K-penetration test before the treatment of the olivine, and the electron microscopic crack graph (b) of example 4.\|[0027] FIG. 7 is a simulation result after 2 years for different injection fluid temperatures and initial olivine temperatures in example 5, showing the results of geology indirect carbonization (Indirect) and geology Direct carbonization (Direct), respectively, wherein (a) is the average olivine temperature rise (in units:. Degree.C.); (b) The average CO 2 sequestration rate (unit: kg/(year. M 3)).\|[0028] Fig. 8 is a graph showing the effect of extracting nickel and cobalt as valuable elements in example 6.\|INVENTION MODE\|The specific embodiment is as follows:\|[0029] The following examples are further illustrative of the invention and are not intended to be limiting thereof. \|[0030] Unless defined otherwise, all technical and scientific terms used hereinafter have the same meaning as commonly understood by one of ordinary skill in the art. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the scope of the present invention. Unless otherwise indicated, the experimental materials and reagents herein are all commercially available products conventional in the art.\|[0031] As shown in fig. 1, a method for permanently sequestering carbon dioxide and simultaneously generating geothermal heat and extracting valuable elements by using geological rock assisted by ammonium bisulfate mainly relates to conventional geological drilling operation, pressurized injection of mixed fluid of CO 2 and ammonium bisulfate, drilling sealing, opening the drilling sealing after reaction is mature, and collecting steam and nickel-cobalt solution. The method specifically comprises the following steps:\|[0032] (1) Selecting injection and screening formation conditions: different injection conditions and stratum conditions bring different geological mineral carbonization effects, corresponding injection conditions are selected in different stratum conditions to improve the energy utilization rate, and the stratum conditions comprise: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, the stratum mineral volume is 1-1 multiplied by 10 20m3, and the injection conditions of the mixed fluid of carbon dioxide and ammonium bisulfate comprise: the liquid temperature is 20-200 ℃, the carbon dioxide pressure is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection; \|[0033] (2) Under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade. \|[0034] Example 1\|[0035] The analysis results of the components of the olivine adopted by the invention are shown in table 1, the NH 4HSO4 amount required for implementation is calculated according to the magnesium, calcium and iron contents, the theoretical carbonation capacity of the olivine mineral is calculated according to the total content of the magnesium, calcium and iron contents in the olivine, and the extractable nickel and cobalt amounts in each ton of olivine are respectively 3.31kg and 0.185kg. Figure 2 shows the X-ray diffraction spectrum of olivine showing that the main mineral composition in the rock sample is olivine Mg 2SiO4, accompanied by small amounts of chrysotile Mg 3Si2O5(OH)4, talc Mg 3Si4O10(OH)2 and iron oxide Fe 2O3. Fig. 3 shows the electron microscope and main element scan results of the olivine, showing the elemental distribution of magnesium, oxygen, silicon, respectively, on the rock surface, demonstrating that magnesium is primarily present in the silicate in the rock.\|[0036] TABLE 1 analysis of elements of olivine samples based on X-ray fluorescence spectra\|[0037] Element/OxideSiO2MgOFe2O3Al2O3CaOCr2O3NiOCoCuOTiO2wt%43.4837.248.570.700.500.470.330.020.010.01\|[0038] Example 2\|[0039] According to the center combination experimental design principle of Box-Benhnken, three factors which have obvious and common influence on magnesium reaction rate are selected, a three-factor three-level response surface analysis method is adopted on the basis of a single-factor experiment, and the experimental factors and the level design are shown in Table 2. FIG. 4 presents a response surface and contour plot of two-factor interaction versus magnesium response rate, which shows a significant logarithmic relationship between magnesium response rate and overall independent variables. The contour diagram shows that the extreme value exists under the conditions that the concentration of NH 4HSO4 is 1.62mol/L, the reaction temperature is 144 ℃ and the solid-liquid ratio is 30g/L, the theoretical magnesium reaction rate can reach 100%, the olivine magnesium extraction experiment is carried out by adopting the experimental conditions, the actual extraction rate is 95%, the relative error is about 5%, and the condition parameters obtained by the response surface analysis method are proved to be accurate and reliable. Comparing the three groups of graphs shows that the solid-liquid ratio has the most obvious effect on the magnesium extraction rate, the concentration of NH 4HSO4 is inferior, and the difference effect of the reaction temperature on the result is smaller.\|[0040] TABLE 2 response surface analysis factors and levels\|[0041] \|[0042] Example 3\|[0043] The NH 4HSO4 concentration and the experimental temperature were varied, and after 15s the solution was extracted and the magnesium content was measured to calculate the reaction rate, and the reaction conditions are shown in Table 3. FIG. 5 shows the trend of the surface reaction rate of olivine with NH 4HSO4 over NH 4HSO4 and 1/T, showing that the surface reaction rate of acid rock increases logarithmically with increasing concentration of NH 4HSO4 and exponentially with increasing temperature, we obtain a reaction progression of 0.462, a reaction activation energy of 36598J/mol, and a frequency factor of 0.184 using the fit equation and Arrhenius equation. Kinetic rate equation for extracting Mg by NH 4HSO4 reacting with the surface of olivine:\|[0044] \|[0045] Wherein J is the surface reaction rate (unit: mol/(cm 2. Multidot. S)), T is the reaction temperature (unit: DEG C), and C NH4HSO4 is the NH 4HSO4 concentration (unit: mol/L). \|[0046] TABLE 3 acid rock surface reaction conditions\|[0047] \|[0048] Example 4\|[0049] Taking the CO 2 phase-change jet fracturing method as an example, the permeability test and SEM test of CO 2 gas measurement before and after treatment are performed on the olivine core sample, and the permeability test results and SEM crack diagrams of the cores before and after treatment are shown in fig. 6. Experimental results showed that the permeability of the untreated sample was 0.1472uD (1 uD = 1 x 10 -3um2); after applying an overburden pressure of 12Mpa (equivalent to a geostatic pressure of about 500m depth) and heating to 40 ℃, the permeability was increased to 0.3862uD by CO 2 jet treatment at 14Mpa pressure, 2.62 times higher than the untreated sample. SEM test results show that the pore structure of the core slice is obviously changed before and after treatment, the crack depth is obviously deepened, and the number of cracks is obviously increased. Experiments prove that the CO 2 phase-change jet fracturing method can improve the permeability of rock.\|[0050] Example 5\|[0051] The average temperature of the stratum at 1000m is set to be 37 ℃, because the optimal temperature of geological direct carbonization is 185 ℃ and the middle point temperature is 90 ℃, 10 days are required for waiting for reaction maturation time after injection at the mixed fluid temperature of 150 ℃ and the carbon dioxide pressure of 20MPa, the concentration of NH 4HSO4 in the mixed fluid is 0.5mol/L, and the solid-to-liquid ratio of the solution of the olivine and NH 4HSO4 is 200kg/L. Figure 7 details the average olivine temperature rise and average CO 2 sequestration rate change after 2 years of geologically indirect carbonization and geologically direct carbonization. The calculation results show that the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization both tend to rise and then fall under the condition of considering heat dissipation, probably because the NH 4HSO4 endothermic decomposition temperature limits the area temperature rise. The average temperature rise of the olivine and the average CO 2 sequestration rate extreme value of the geology indirect carbonization are found at t0=90 ℃, tin=185 ℃, and are respectively 181 ℃ and 195 kg/(year-m 3), the average temperature of the olivine and the annual carbon sequestration quantity respectively reach 271 ℃ and 19.5 ten thousand tons, and the average temperature rise of the olivine and the annual carbon sequestration rate extreme value are improved by more than 60% compared with the lowest case (t0=37 ℃, tin=37 ℃). When T0 is the same, the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization are both in an ascending trend along with the increase of Tin. Compared with two mineral carbonization modes, when T0 and Tin are at lower temperature, the average olivine temperature rise and the average CO 2 sealing rate of the geology indirect carbonization are far greater than those of the geology indirect carbonization; when T0 and Tin are at higher temperatures, the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization are both higher than those of the geology direct carbonization, but the gap is reduced, and only when the T0 temperature is lower and the Tin temperature is higher, the average olivine temperature rise of the geology direct carbonization can exceed that of the geology indirect carbonization. This introduces a feature of geological indirect carbonization.\|[0052] As can be seen from fig. 7, the result of geologically indirect carbonization is less sensitive to temperature than geologically direct carbonization, which suggests that it has the potential to be applied to shallow olivine, since shallow olivine formations typically have lower initial temperatures. Taking the case of t0=37 ℃ and tin=37 ℃ which are easy to reach underground and ground as an example, the annual carbon sequestration amount can reach 19.5 ten thousand tons, approaching the optimal effect of geological direct carbonization in computation, the temperature of the olive strata can rise to 142 ℃ after 2 years, approaching the high-temperature geothermal grade, the stratum temperature level is only common in dry hot rocks deep in the earth at present, the depth is generally more than 3000m, and high drilling cost and fluid compression power consumption are required for developing the resource.\|[0053] Example 6\|[0054] Under the sealing conditions of example 5, other conditions are unchanged, ammonium bisulfate is replaced by HCl, HF, NH 4 Cl or NH 4HCO3, the extraction effect on high-value cobalt nickel element is compared, namely NH 4HSO4、HCl、HF、NH4 Cl or NH 4HCO3 is recovered, and the extraction efficiency of cobalt nickel element is detected, as shown in figure 8.\|[0055] As shown in Table 8, the extraction effect of NH 4SO4 and HCl on cobalt and nickel elements is equivalent, and because HCl is strong acid and is harmful to the environment, pollution is caused to water and soil, and the extraction efficiency of valuable elements nickel and cobalt is up to 90 percent by using ammonium bisulfate to assist in utilizing geological rock to seal carbon dioxide.\|[0056] Example 7\|[0057] An ammonium bisulfate assisted method for permanently sequestering carbon dioxide by using geological rock while generating geothermal heat and extracting valuable elements comprises the following steps: selecting injection and screening formation conditions: the formation conditions include: the injection conditions of the mixed fluid of the carbon dioxide and the ammonium bisulfate comprise that the underground depth is 0m, the surface temperature is 20 ℃, the formation flow pressure is 0.1MPa, the formation porosity is 50%, the formation permeability is 1 multiplied by 10 -2m2, the formation mineral volume is 1 to 1 multiplied by 10 20m3: the temperature of the mixed fluid is 20 ℃, the pressure of carbon dioxide is 0.1MPa, and the reaction maturation time is waited for 12 hours after injection; under the assistance of ammonium bisulfate, the mixed fluid of ammonium bisulfate and carbon dioxide is injected to react with the olivine through seepage and mass transfer to quickly generate stable carbonate, and meanwhile, high-value elements of nickel and cobalt rich in magnesium, calcium and iron silicate of the leaching solution are recovered.\|[0058] Example 8\|[0059] An ammonium bisulfate assisted method for permanently sequestering carbon dioxide by using geological rock while generating geothermal heat and extracting valuable elements comprises the following steps: selecting injection and screening formation conditions: the formation conditions include: the injection conditions of the mixed fluid of the carbon dioxide and the ammonium bisulfate comprise: the temperature of the mixed fluid is 200 ℃, the pressure of carbon dioxide is 40MPa, and the reaction maturation time is 3650 days after injection; under the assistance of ammonium bisulfate, the mixed fluid of ammonium bisulfate and carbon dioxide is injected to react with the olivine through seepage and mass transfer to quickly generate stable carbonate, and meanwhile, high-value elements of nickel and cobalt rich in magnesium, calcium and iron silicate of the leaching solution are recovered.\|[0060] The above embodiments are only described to assist in understanding the technical solution of the present invention and its core idea, and it should be noted that it will be obvious to those skilled in the art that several improvements and modifications can be made to the present invention without departing from the principle of the present invention, and these improvements and modifications also fall within the protection scope of the claims of the present invention.	(CN118189424)\|TECHNICAL FIELD\|[0001] The invention relates to the technical field of carbon dioxide sequestration, in particular to a method for generating geothermal heat and extracting valuable elements by permanently sequestering carbon dioxide by using geological rock with the aid of ammonium bisulfate. \|BACKGROUND ART\|The background technology is as follows:\|[0002] large scale carbon capture, utilization and sequestration (CCUS) technologies must be developed to achieve carbon neutralization, which involves injection of CO 2 into geological structures, such as deep brine layers or Enhanced Oil Recovery (EOR) in oil fields, but may involve leakage of freely stored CO 2 back to the atmosphere. \|[0003] The invention applied by the inventor realizes permanent fixation by utilizing the reaction of silicate minerals rich in magnesium, calcium and iron in geological strata and CO 2, but the risk of leakage of CO 2 back to the atmosphere can be greatly reduced and heat release is also accompanied; however, this process is very slow, and it is difficult and long time to accumulate valuable heat energy for use under the heat dissipation conditions of the geological structure, and the geological sequestration depth of CO 2 is generally better in the range of 2000-3000 meters, and this depth brings about thresholds such as drilling cost, compression energy consumption of CO 2, and the like.\|[0004] In view of the fact that geothermal energy has become one of the most competitive renewable energy utilization modes, the CO 2 geological sequestration is indeed capable of generating geothermal-like heat for utilization, and a new method is needed to achieve carbon dioxide sequestration while improving geothermal grade.\|DISCLOSURE\|The invention comprises the following steps:\|[0005] Aiming at the problems existing in the prior art, the invention provides a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide assisted by ammonium bisulfate, which can obviously accelerate the carbonization reaction path of minerals in stratum, accelerate heat release by faster reaction, drive considerable temperature rise of the rock and improve geothermal grade and economic benefit feasibility of heat collection. \|[0006] The invention aims to provide a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which comprises the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid.\|[0007] The invention discloses a carbonization reaction path capable of remarkably accelerating minerals in a stratum, accelerating heat release by faster reaction, driving considerable temperature rise of rock, and improving geothermal grade and economic benefit feasibility of heat collection. According to the invention, strong acid weak alkali salt (ammonium bisulfate NH 4HSO4) is adopted to accelerate the reaction of magnesium calcium silicate in a geological structure and injected CO 2, NH 4HSO4 has the potential of recycling, nickel and cobalt high-value elements rich in magnesium, calcium and iron silicate in leaching liquid are recovered, the nickel and cobalt productivity is improved to meet the requirements of clean energy sources of electric automobiles, the carbon footprint in mining activities is reduced, and high-purity amorphous silicon dioxide and brucite produced by subsequent processing of the solution can also be used for other chemical production.\|[0008] The method provided by the invention is characterized in that under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade.\|[0009] Preferably, the method specifically comprises the following steps: injecting a mixed fluid of ammonium bisulfate and carbon dioxide into a stratum of silicate minerals containing magnesium, calcium and iron, reacting the mixed fluid with the silicate minerals containing magnesium, calcium and iron to generate carbonate, permanently sealing carbon dioxide, simultaneously coupling heat release and reaction rate to improve geothermal grade, and recovering valuable elements nickel and cobalt rich in silicate in the leaching solution.\|[0010] The method provided by the invention is to inject the mixed fluid of CO 2 and ammonium bisulfate into a well, seal the well, open the well after the reaction is mature, collect steam and nickel-cobalt solution, realize that geological rock permanently seals carbon dioxide to generate geothermal heat and extract valuable elements nickel-cobalt.\|[0011] The invention continuously pushes the proposed silicate minerals which are rich in magnesium, calcium and iron in geological strata to react with CO 2 to realize permanent fixation technology, adopts strong acid weak alkali salt (such as ammonium bisulfate NH 4HSO4), accelerates the reaction of magnesium calcium silicate rock in geological structures with injected CO 2, and NH 4HSO4 has recoverable recycling potential, simultaneously recovers nickel and cobalt high-value elements which are rich in magnesium, calcium and iron silicate in leaching solution, improves the nickel and cobalt capacity to meet the requirements of clean energy of electric vehicles, reduces the carbon footprint in mining activities, ensures that the high-purity amorphous silicon dioxide and brucite which are produced by subsequent processing of the solution can also be used for other chemical production, changes the defect of very slow conventional permanent sealing reaction rate, improves the sealing geological grade, simultaneously reduces the sealing geological depth, and obtains high-value elements including recovered nickel and cobalt, reduces the cost, the compression energy consumption of CO 2 and the like.\|[0012] Preferably, the formation conditions include: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3. Different injection conditions and stratum conditions bring different geological mineral carbonization effects, and corresponding injection conditions are selected under different stratum conditions, so that the energy utilization rate is improved. Further preferably, the formation conditions include: the underground depth is 1000-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3.\|[0013] Preferably, the injection conditions of the mixed fluid of ammonium bisulfate and carbon dioxide comprise: the temperature of the mixed fluid is 20-200 ℃, the pressure of carbon dioxide is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection.\|[0014] Preferably, the geothermal grade is a medium and high temperature geothermal grade greater than 150 ℃.\|[0015] Preferably, the silicate minerals include olivine, serpentine, basalt, wollastonite and anorthite which are rich in magnesium, calcium and iron.\|[0016] Preferably, the concentration of NH 4HSO4 in the mixed fluid is 0.1-2.0mol/L, the solid-to-liquid ratio of silicate mineral to NH 4HSO4 solution is 100-1000kg/L, and the reaction temperature is 50-180 ℃.\|[0017] The invention also protects the application of the method in carbon dioxide sequestration.\|[0018] Compared with the prior art, the invention has the following advantages:\|[0019] 1. According to the method provided by the invention, in the geological rock and 2-year period, the initial temperature of the related geological rock stratum and the temperature of the CO 2 fluid injected are 37 ℃ and 1 cubic kilometer, the average temperature rise of the rock can reach 105 ℃ and reach 142 ℃ at the final temperature, high geothermal grade reaction heat is generated, and meanwhile, the geological storage CO 2 amount can reach 11.9 ten thousand tons each year, which is equivalent to the annual carbon storage amount of 342k square kilometer forests in northwest China; if the temperature of the fluid injected with CO 2 and the initial rock temperature are further increased to 90 ℃, the rock temperature rise and the average CO 2 sealing rate are increased by more than 60% compared with those at 37 ℃, the rock temperature after 2 years is increased by 181 ℃, and the grade of the high-temperature geothermal grade is far more than 150 ℃. Meanwhile, the extraction efficiency of valuable elements nickel and cobalt exceeds 50%, the total CO 2 sealing benefit, geothermal benefit and valuable element mining and smelting benefit are obtained, and each sealing 1 ton of CO 2 can obtain remarkable economic benefit, so that the high cost situation of CO 2 geological sealing is thoroughly twisted. \|[0020] 2. The method provided by the invention is characterized in that under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade.\|DRAWINGS DESCRIPTION\|Description of the drawings:\|[0021] FIG. 1 is a schematic view of a geological vertical section of the invention with ammonium bisulfate assisted permanent sequestration of CO 2 while producing geothermal heat and extracting valuable elements. \|[0022] Fig. 2 is an X-ray diffraction spectrum of the sample of olivine of example 1.\|[0023] FIG. 3 is an electron microscopy image (a) and elemental scan spectra (b-d) of the olivine flakes of example 1.\|[0024] FIG. 4 is a plot of response surface and contour of the two-factor interaction versus magnesium response rate in example 2.\|[0025] FIG. 5 is a graph showing the surface reaction rate of the olivine with NH 4HSO4 as a function of (a) NH 4HSO4 and (b) 1/T in example 3.\|[0026] FIG. 6 is a graph of the K-penetration (c) after the treatment of the olivine, showing the results (a) of the K-penetration test before the treatment of the olivine, and the electron microscopic crack graph (b) of example 4.\|[0027] FIG. 7 is a simulation result after 2 years for different injection fluid temperatures and initial olivine temperatures in example 5, showing the results of geology indirect carbonization (Indirect) and geology Direct carbonization (Direct), respectively, wherein (a) is the average olivine temperature rise (in units:. Degree.C.); (b) The average CO 2 sequestration rate (unit: kg/(year. M 3)).\|[0028] Fig. 8 is a graph showing the effect of extracting nickel and cobalt as valuable elements in example 6.\|INVENTION MODE\|The specific embodiment is as follows:\|[0029] The following examples are further illustrative of the invention and are not intended to be limiting thereof. \|[0030] Unless defined otherwise, all technical and scientific terms used hereinafter have the same meaning as commonly understood by one of ordinary skill in the art. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the scope of the present invention. Unless otherwise indicated, the experimental materials and reagents herein are all commercially available products conventional in the art.\|[0031] As shown in fig. 1, a method for permanently sequestering carbon dioxide and simultaneously generating geothermal heat and extracting valuable elements by using geological rock assisted by ammonium bisulfate mainly relates to conventional geological drilling operation, pressurized injection of mixed fluid of CO 2 and ammonium bisulfate, drilling sealing, opening the drilling sealing after reaction is mature, and collecting steam and nickel-cobalt solution. The method specifically comprises the following steps:\|[0032] (1) Selecting injection and screening formation conditions: different injection conditions and stratum conditions bring different geological mineral carbonization effects, corresponding injection conditions are selected in different stratum conditions to improve the energy utilization rate, and the stratum conditions comprise: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, the stratum mineral volume is 1-1 multiplied by 10 20m3, and the injection conditions of the mixed fluid of carbon dioxide and ammonium bisulfate comprise: the liquid temperature is 20-200 ℃, the carbon dioxide pressure is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection; \|[0033] (2) Under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade. \|[0034] Example 1\|[0035] The analysis results of the components of the olivine adopted by the invention are shown in table 1, the NH 4HSO4 amount required for implementation is calculated according to the magnesium, calcium and iron contents, the theoretical carbonation capacity of the olivine mineral is calculated according to the total content of the magnesium, calcium and iron contents in the olivine, and the extractable nickel and cobalt amounts in each ton of olivine are respectively 3.31kg and 0.185kg. Figure 2 shows the X-ray diffraction spectrum of olivine showing that the main mineral composition in the rock sample is olivine Mg 2SiO4, accompanied by small amounts of chrysotile Mg 3Si2O5(OH)4, talc Mg 3Si4O10(OH)2 and iron oxide Fe 2O3. Fig. 3 shows the electron microscope and main element scan results of the olivine, showing the elemental distribution of magnesium, oxygen, silicon, respectively, on the rock surface, demonstrating that magnesium is primarily present in the silicate in the rock.\|[0036] TABLE 1 analysis of elements of olivine samples based on X-ray fluorescence spectra\|[0037] Element/OxideSiO2MgOFe2O3Al2O3CaOCr2O3NiOCoCuOTiO2wt%43.4837.248.570.700.500.470.330.020.010.01\|[0038] Example 2\|[0039] According to the center combination experimental design principle of Box-Benhnken, three factors which have obvious and common influence on magnesium reaction rate are selected, a three-factor three-level response surface analysis method is adopted on the basis of a single-factor experiment, and the experimental factors and the level design are shown in Table 2. FIG. 4 presents a response surface and contour plot of two-factor interaction versus magnesium response rate, which shows a significant logarithmic relationship between magnesium response rate and overall independent variables. The contour diagram shows that the extreme value exists under the conditions that the concentration of NH 4HSO4 is 1.62mol/L, the reaction temperature is 144 ℃ and the solid-liquid ratio is 30g/L, the theoretical magnesium reaction rate can reach 100%, the olivine magnesium extraction experiment is carried out by adopting the experimental conditions, the actual extraction rate is 95%, the relative error is about 5%, and the condition parameters obtained by the response surface analysis method are proved to be accurate and reliable. Comparing the three groups of graphs shows that the solid-liquid ratio has the most obvious effect on the magnesium extraction rate, the concentration of NH 4HSO4 is inferior, and the difference effect of the reaction temperature on the result is smaller.\|[0040] TABLE 2 response surface analysis factors and levels\|[0041] \|[0042] Example 3\|[0043] The NH 4HSO4 concentration and the experimental temperature were varied, and after 15s the solution was extracted and the magnesium content was measured to calculate the reaction rate, and the reaction conditions are shown in Table 3. FIG. 5 shows the trend of the surface reaction rate of olivine with NH 4HSO4 over NH 4HSO4 and 1/T, showing that the surface reaction rate of acid rock increases logarithmically with increasing concentration of NH 4HSO4 and exponentially with increasing temperature, we obtain a reaction progression of 0.462, a reaction activation energy of 36598J/mol, and a frequency factor of 0.184 using the fit equation and Arrhenius equation. Kinetic rate equation for extracting Mg by NH 4HSO4 reacting with the surface of olivine:\|[0044] \|[0045] Wherein J is the surface reaction rate (unit: mol/(cm 2. Multidot. S)), T is the reaction temperature (unit: DEG C), and C NH4HSO4 is the NH 4HSO4 concentration (unit: mol/L). \|[0046] TABLE 3 acid rock surface reaction conditions\|[0047] \|[0048] Example 4\|[0049] Taking the CO 2 phase-change jet fracturing method as an example, the permeability test and SEM test of CO 2 gas measurement before and after treatment are performed on the olivine core sample, and the permeability test results and SEM crack diagrams of the cores before and after treatment are shown in fig. 6. Experimental results showed that the permeability of the untreated sample was 0.1472uD (1 uD = 1 x 10 -3um2); after applying an overburden pressure of 12Mpa (equivalent to a geostatic pressure of about 500m depth) and heating to 40 ℃, the permeability was increased to 0.3862uD by CO 2 jet treatment at 14Mpa pressure, 2.62 times higher than the untreated sample. SEM test results show that the pore structure of the core slice is obviously changed before and after treatment, the crack depth is obviously deepened, and the number of cracks is obviously increased. Experiments prove that the CO 2 phase-change jet fracturing method can improve the permeability of rock.\|[0050] Example 5\|[0051] The average temperature of the stratum at 1000m is set to be 37 ℃, because the optimal temperature of geological direct carbonization is 185 ℃ and the middle point temperature is 90 ℃, 10 days are required for waiting for reaction maturation time after injection at the mixed fluid temperature of 150 ℃ and the carbon dioxide pressure of 20MPa, the concentration of NH 4HSO4 in the mixed fluid is 0.5mol/L, and the solid-to-liquid ratio of the solution of the olivine and NH 4HSO4 is 200kg/L. Figure 7 details the average olivine temperature rise and average CO 2 sequestration rate change after 2 years of geologically indirect carbonization and geologically direct carbonization. The calculation results show that the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization both tend to rise and then fall under the condition of considering heat dissipation, probably because the NH 4HSO4 endothermic decomposition temperature limits the area temperature rise. The average temperature rise of the olivine and the average CO 2 sequestration rate extreme value of the geology indirect carbonization are found at t0=90 ℃, tin=185 ℃, and are respectively 181 ℃ and 195 kg/(year-m 3), the average temperature of the olivine and the annual carbon sequestration quantity respectively reach 271 ℃ and 19.5 ten thousand tons, and the average temperature rise of the olivine and the annual carbon sequestration rate extreme value are improved by more than 60% compared with the lowest case (t0=37 ℃, tin=37 ℃). When T0 is the same, the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization are both in an ascending trend along with the increase of Tin. Compared with two mineral carbonization modes, when T0 and Tin are at lower temperature, the average olivine temperature rise and the average CO 2 sealing rate of the geology indirect carbonization are far greater than those of the geology indirect carbonization; when T0 and Tin are at higher temperatures, the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization are both higher than those of the geology direct carbonization, but the gap is reduced, and only when the T0 temperature is lower and the Tin temperature is higher, the average olivine temperature rise of the geology direct carbonization can exceed that of the geology indirect carbonization. This introduces a feature of geological indirect carbonization.\|[0052] As can be seen from fig. 7, the result of geologically indirect carbonization is less sensitive to temperature than geologically direct carbonization, which suggests that it has the potential to be applied to shallow olivine, since shallow olivine formations typically have lower initial temperatures. Taking the case of t0=37 ℃ and tin=37 ℃ which are easy to reach underground and ground as an example, the annual carbon sequestration amount can reach 19.5 ten thousand tons, approaching the optimal effect of geological direct carbonization in computation, the temperature of the olive strata can rise to 142 ℃ after 2 years, approaching the high-temperature geothermal grade, the stratum temperature level is only common in dry hot rocks deep in the earth at present, the depth is generally more than 3000m, and high drilling cost and fluid compression power consumption are required for developing the resource.\|[0053] Example 6\|[0054] Under the sealing conditions of example 5, other conditions are unchanged, ammonium bisulfate is replaced by HCl, HF, NH 4 Cl or NH 4HCO3, the extraction effect on high-value cobalt nickel element is compared, namely NH 4HSO4、HCl、HF、NH4 Cl or NH 4HCO3 is recovered, and the extraction efficiency of cobalt nickel element is detected, as shown in figure 8.\|[0055] As shown in Table 8, the extraction effect of NH 4SO4 and HCl on cobalt and nickel elements is equivalent, and because HCl is strong acid and is harmful to the environment, pollution is caused to water and soil, and the extraction efficiency of valuable elements nickel and cobalt is up to 90 percent by using ammonium bisulfate to assist in utilizing geological rock to seal carbon dioxide.\|[0056] Example 7\|[0057] An ammonium bisulfate assisted method for permanently sequestering carbon dioxide by using geological rock while generating geothermal heat and extracting valuable elements comprises the following steps: selecting injection and screening formation conditions: the formation conditions include: the injection conditions of the mixed fluid of the carbon dioxide and the ammonium bisulfate comprise that the underground depth is 0m, the surface temperature is 20 ℃, the formation flow pressure is 0.1MPa, the formation porosity is 50%, the formation permeability is 1 multiplied by 10 -2m2, the formation mineral volume is 1 to 1 multiplied by 10 20m3: the temperature of the mixed fluid is 20 ℃, the pressure of carbon dioxide is 0.1MPa, and the reaction maturation time is waited for 12 hours after injection; under the assistance of ammonium bisulfate, the mixed fluid of ammonium bisulfate and carbon dioxide is injected to react with the olivine through seepage and mass transfer to quickly generate stable carbonate, and meanwhile, high-value elements of nickel and cobalt rich in magnesium, calcium and iron silicate of the leaching solution are recovered.\|[0058] Example 8\|[0059] An ammonium bisulfate assisted method for permanently sequestering carbon dioxide by using geological rock while generating geothermal heat and extracting valuable elements comprises the following steps: selecting injection and screening formation conditions: the formation conditions include: the injection conditions of the mixed fluid of the carbon dioxide and the ammonium bisulfate comprise: the temperature of the mixed fluid is 200 ℃, the pressure of carbon dioxide is 40MPa, and the reaction maturation time is 3650 days after injection; under the assistance of ammonium bisulfate, the mixed fluid of ammonium bisulfate and carbon dioxide is injected to react with the olivine through seepage and mass transfer to quickly generate stable carbonate, and meanwhile, high-value elements of nickel and cobalt rich in magnesium, calcium and iron silicate of the leaching solution are recovered.\|[0060] The above embodiments are only described to assist in understanding the technical solution of the present invention and its core idea, and it should be noted that it will be obvious to those skilled in the art that several improvements and modifications can be made to the present invention without departing from the principle of the present invention, and these improvements and modifications also fall within the protection scope of the claims of the present invention.	Family Number\|(110191082)\|110191082\|Object of Invention\|(CN118189424 A)\|The invention relates to the technical field of carbon dioxide sequestration , in particular to a method for generating geothermal heat and extracting valuable elements by permanently sequestering carbon dioxide by using geological rock with the aid of ammonium bisulfate . \|Abstract\|(CN118189424 A)\|The invention discloses a method for generating terrestrial heat and extracting valuable elements by permanently sealing and storing carbon dioxide through geological rocks under the assistance of ammonium bisulfate . The method comprises the following steps that under the assistance of ammonium bisulfate , silicate rock minerals containing magnesium , calcium and iron in a geologic structure react with injected carbon dioxide , carbon dioxide is permanently sealed , meanwhile , terrestrial heat is generated , and valuable elements rich in leachate silicate are recycled . According to the method , under the assistance of ammonium bisulfate , injected carbon dioxide mixed liquid reacts with silicate geological minerals containing magnesium , calcium and iron through seepage and mass transfer , stable carbonate is rapidly generated , the mineralization fixing process is fast , meanwhile , heat release and the reaction rate are coupled to improve the geothermal grade , the reaction is accelerated through ammonium bisulfate , the mineralization reaction rate is increased , and the mineralization effect is improved . The heat release process of the mineral carbonization reaction is coupled with the reaction rate to improve the geothermal grade . \|	Materials, metallurgy\|Thermal processes and apparatus	C01B-033/12/6\|C01F-005/14\|C01G-051/00\|C01G-053/00\|C01P-2006/80\|C22B-003/04\|C22B-023/0415\|F24T-010/00\|F24V-030/00\|F28D-020/00/52		C01B-033/12/6\|C01F-005/14\|C01G-051/00\|C01G-053/00\|C01P-2006/80\|C22B-003/04\|C22B-023/0415\|F24T-010/00\|F24V-030/00\|F28D-020/00/52	C01B-033/12\|C01F-005/14\|C01G-051/00\|C01G-053/00\|C22B-003/04\|C22B-023/00\|F24T-010/00\|F24V-030/00\|F28D-020/00	C01B-033/12\|C01F-005/14\|C01G-051/00\|C01G-053/00\|C22B-003/04\|C22B-023/00\|F24T-010/00\|F24V-030/00\|F28D-020/00			CN118423599	CN118423599 110862844 WHO=Examiner SELF=N CAT=A						PENDING	(CN118189424)\|PENDING	ALIVE	(CN118189424)\|ALIVE	(CN118189424)\|LEGAL DETAILS FOR CN118189424\|Actual or expected expiration date=2044-03-15\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-15\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202410297703\|Application date=2024-03-15\|Standardized application number=2024CN-0297703\|Event publication date=2024-06-14\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN118189424\|Publication stage code=A\|Publication date=2024-06-14\|Standardized publication number=CN118189424\|Event publication date=2024-06-14\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2024-07-02\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN118189424)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTO/ioLPE5/vlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000073203207&ekey=2149&xpn=CN118189424&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=PBZzTIHmhIfplFjK9nH8lZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN118189424)\|CN	(CN118189424)\|NAME=GUANGZHOU INSTITUTE OF ENERGY CONVERSION CHINESE ACADEMY OF SCIENCES , COUNTRY=CN		(CN118189424)\|NAME=FANG YAN;GUANGZHOU KEYUE I.P. LAW OFFICE , REG=44001NAME=MO YAOJIANG;GUANGZHOU KEYUE I.P. LAW OFFICE , REG=44001		(CN118189424)\|NAME=CAO YAN	(CN118189424)\|8	1	1					(CN118189424)\|Number of Claims: NCL=8\|Gazette date: GAZDATE=2024-06-14\|Gazette number: GAZNUM=40-2402\|Number of Pages: NPAGES=14\|		(CN118189424)\|CHINESE (CHI)	(CN118189424)\|Patent	Titre: (CN118189424)\|Method for generating terrestrial heat and extracting valuable elements by permanently sealing carbon dioxide through geological rock under assistance of ammonium bisulfate Résumé: (CN118189424)\|The invention discloses a method for generating terrestrial heat and extracting valuable elements by permanently sealing and storing carbon dioxide through geological rocks under the assistance of ammonium bisulfate. The method comprises the following steps that under the assistance of ammonium bisulfate, silicate rock minerals containing magnesium, calcium and iron in a geologic structure react with injected carbon dioxide, carbon dioxide is permanently sealed, meanwhile, terrestrial heat is generated, and valuable elements rich in leachate silicate are recycled. According to the method, under the assistance of ammonium bisulfate, injected carbon dioxide mixed liquid reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is rapidly generated, the mineralization fixing process is fast, meanwhile, heat release and the reaction rate are coupled to improve the geothermal grade, the reaction is accelerated through ammonium bisulfate, the mineralization reaction rate is increased, and the mineralization effect is improved. The heat release process of the mineral carbonization reaction is coupled with the reaction rate to improve the geothermal grade.	27	Abstract	gpt-4o-mini	yes	The method involves the reaction of silicate rock minerals with injected CO₂ to generate stable carbonates, which aligns with the goal of carbon sequestration and enhanced weathering.
32	SG2013095575\|WOSG2014/000613\|SG11201605164Y	WOSG2014/000613\|AU2014370454\|US15/107,870\|SG11201605164Y	AU2014370454\|US9896741\|US20160319395\|SG11201605164Y\|AU2014370454\|SG11201605164Y\|WO2015/099612	69805816	WO2015/099612 A1 2015-07-02 [WO201599612]\|AU2014370454 B2 2019-05-16 [AU2014370454]\|AU2014370454 A1 2016-07-28 [AU2014370454]\|US9896741 B2 2018-02-20 [US9896741]\|US20160319395 A1 2016-11-03 [US20160319395]\|SG11201605164Y B 2016-10-31 [SG11201605164Y]\|SG11201605164Y A 2016-07-28 [SG11201605164Y]	2013-12-24\|2014-12-23	2014-12-23\|2014-12-23\|2014-12-23\|2014-12-23	2019-05-16\|2018-02-20\|2016-11-03\|2016-10-31\|2016-07-28\|2016-07-28\|2015-07-02	(US9896741)\|2018-02-20\|\|(AU2014370454)\|2019-05-16\|(SG11201605164Y)\|2016-10-31	(US9896741)\|2035-01-20\|(WO2015/099612)\|2017-06-24\|(AU2014370454)\|2034-12-23\|(SG11201605164Y)\|2034-12-23	(US9896741)\|Method of producing metal carbonate from an ultramafic rock material	(US9896741)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.	A STAR - AGENCY FOR SCIENCE TECHNOLOGY & RESEARCH	(US9896741)\|Agency for Science, Technology and Research ([SG])\|(US20160319395)\|Agency for Science, Technology and Research ([SG])\|(WO2015/099612)\|AGENCY FOR SCIENCE, TECHNOLOGY AND RESEARCH ([SG])\|(AU2014370454)\|Agency for Science, Technology and Research\|(AU2014370454)\|Agency for Science, Technology and Research\|(SG11201605164Y)\|AGENCY FOR SCIENCE, TECHNOLOGY AND RESEARCH ([SG])\|(SG11201605164Y)\|AGENCY FOR SCIENCE, TECHNOLOGY AND RESEARCH ([SG])	BU JIE\|YEO TZE YUEN\|SHARRATT PAUL	(US9896741)\|Bu Jie\|Yeo Tze Yuen\|Sharratt Paul\|(US20160319395)\|Bu Jie\|Yeo Tze Yuen\|Sharratt Paul	(US9896741)\|Winstead, P.C.\|(WO2015/099612)\|VIERING, JENTSCHURA & PARTNER LLP ([SG])\|(AU2014370454)\|Phillips Ormonde Fitzpatrick ([AU])\|(SG11201605164Y)\|VIERING, JENTSCHURA & PARTNER LLP ([SG])\|Reg. Nb: T06LL1666B	(US9896741)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|Iron (III) oxide may be precipitated out from the mixture following oxidation to allow their easy removal.\|Thus, it is desirable to use concentrated solutions or gases in order to reduce infrastructure and operating costs.\|Since it is nearly impossible to inhibit the co-extraction of these elements during the acid leaching step, it is necessary to remove them in a separate step to separate Fe, Ni, Mn and Cr oxides, which are high value added metal salts, to ensure that high purity magnesite is obtained at the end of the process.\|	(US9896741)\|1. A method of producing a metal carbonate from an ultramafic rock material, the method comprising a) providing an ultramafic rock material comprising a metal silicate; b) reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; c) contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; d) heating the resultant mixture from step c) to decompose the salt of the metal to form metal oxide; and e) reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|16. A system for producing a metal carbonate from ultramafic rock material, the system comprising a) a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal; b) an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; c) a furnace configured to heat the resultant mixture from step b) to decompose the salt of the metal to form the metal oxide; and d) a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|	(US9896741)\|In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided.\|The invention relates to methods of producing metal carbonate from an ultramafic rock material.\|The method of the first aspect includes heating the resultant mixture following contact with oxygen to decompose the salt of the metal to form metal oxide.\|	(US9896741)\|ULTRAMAFIC ROCK MATERIAL(100,36)\|METAL CARBONATE(100,29)\|AERATE IMPURITY(100,9)\|METAL PRODUCTION(100,5)\|PRODUCING METAL CARBONATE(100,5)\|SALT DECOMPOSITION(89,8)\|PURITY MAGNESITE(73,1)\|ULTRAMAFIC ROCK(54,20)\|AQUEOUS CHESHUNT MIXTURE(54,17)\|PRECIPITATOR(46,8)\|ACID RESIDUE(43,10)\|COEXTRACTION(42,1)\|METHANEDIONE(38,22)\|CHESHUNT MIXTURE(36,20)\|CR OXIDE(36,1)\|METHANEDIONE REACTION(32,2)\|AIR STRIPPER COLUMN(30,19)\|METAL SILICATE(30,8)\|RECYCLING(28,4)\|FURNACE(27,10)\|REACTOR(27,6)\|SALT HYDRATION(27,5)\|ACIDIC VAPOR(26,4)\|INFRASTRUCTURE(25,3)\|AQUEOUS AMMONIA MOLAR RATIO(24,2)\|ACID LEACHING(24,1)\|METAL OXIDE(21,21)\|AMBIENT CONDITION(16,2)\|MAFIC MINERAL(15,3)\|MGCL2 6H2O HYDROLYSIS(14,1)\|GAS LIQUID PACKED COLUMN(13,7)\|ULTRAMAFIC ROCK PARTICLE(13,3)\|MGCL2 6H2O MOLE(13,1)\|PACKED SCRUBBING TOWER(13,1)\|HYDROHALIC ACID(12,3)\|CONCENTRATED SOLUTION(12,2)\|MGCL2 4H2O(12,2)\|CO2 EMISSION MITIGATION(11,1)\|NIO MNO PERCENT(11,1)\|CARBONATION REACTION(10,2)\|HEXAHYDRATE SALT(10,2)\|MAXIMAL DIMENSION(10,2)\|ACCELERATE LIBERATION(10,1)\|AQUEOUS AMMONIA FEASIBILITY(10,1)\|CHANGI WWTP(10,1)\|CO2 MINERALIZATION(10,1)\|DECOMPOSITION THERMODYNAMICS(10,1)\|GASEOUS METHANEDIONE(10,1)\|METAIGNEOUS ROCK(10,1)\|METHANEDIONE CAPTURE(10,1)\|NET CO2 CAPTURE(10,1)\|PACKING RESTRAINER(10,1)\|PASIR PANJANG(10,1)\|PULAU SAKRA(10,1)\|PULAU SERAYA(10,1)\|SINGAPORE OLEFIN(10,1)\|SMPO COGEN(10,1)\|SUBGENERIC GROUPING(10,1)\|VAPOR RECOMPRESSOR(10,1)\|MG3SI2O(8,4)\|ACID DIGESTION(8,2)\|AMPLE OPPORTUNITY(8,1)\|INDUSTRY INFRASTRUCTURE(8,1)\|LEACHING REQUIREMENT(8,1)\|MGCL2 2H2O(8,1)\|OPERATING COST(8,1)\|SERPENTINE ORE(8,1)\|SIMULTANEOUS EVAPORATION(8,1)\|STRATEGIC IMPORTANCE(8,1)\|MANGANESE(7,7)\|CHROMIUM(7,6)\|THERMOGRAVIMETRIC ANALYSIS(7,4)\|CO2 REMOVAL(7,3)\|COAL GASIFICATION(7,3)\|REEMISSION(7,3)\|AMMONIA CAPTURE(7,1)\|AQUEOUS LEACHING(7,1)\|CO2 CAPTURE REACTION(7,1)\|CO2 TON(7,1)\|CONCENTRATED LEACHATE SOLUTION(7,1)\|DIHYDRATE SALT(7,1)\|DIVERSE INDUSTRY(7,1)\|KEEPING ELECTRICITY(7,1)\|LEACHATE SOLUTION PH(7,1)\|LEACHATE STREAM(7,1)\|MG DECOMPOSITION(7,1)\|MGO MOL(7,1)\|MINERALIZATION REACTION(7,1)\|PURIFIED LEACHATE SOLUTION(7,1)\|SATURATED LEACHATE SOLUTION(7,1)\|SLOW DEHYDRATION(7,1)\|T CO2 HR TUA(7,1)\|TANK AGITATION(7,1)\|TETRAHYDRATE SALT(7,1)\|VALUE ADDED METAL SALT(7,1)\|HEATED AIR STRIPPER(6,5)\|11H2O(6,2)\|ALKALINE EARTH SILICATE MINERAL(6,2)\|EVAPORATOR(6,2)\|FIRE RETARDANT(6,2)\|HYDROGEN CHLORIDE STRIPPING(6,2)\|LAND RECLAMATION(6,2)\|METAL REFINERY(6,2)\|NEXT DECADE(6,2)\|NITROUS PRODUCT(6,2)\|HEAVY INDUSTRY(5,4)\|STEAM(5,4)\|HEATING MEDIUM(5,3)\|LEACHING(5,3)\|HSC(5,2)\|CARBONATION PRODUCT(5,1)\|COARSE SILICA SOLID RESIDUE(5,1)\|COMMERCIALIZATION(5,1)\|DESIGNED SCRUBBER(5,1)\|EFFLUENT TREATMENT(5,1)\|ELECTROLYTIC PRODUCTION(5,1)\|ESTABLISHED FUNDAMENTAL(5,1)\|GLOBAL METHANEDIONE LEVEL(5,1)\|GLOBAL SCALE(5,1)\|HARTSHORN(5,1)\|HYDRATED METAL SALT CRYSTALIZATION(5,1)\|INORGANIC SAMPLE(5,1)\|IRON OXIDATION(5,1)\|IRON SEPARATING OXIDE(5,1)\|LEACHING MEDIUM(5,1)\|LIQUID REDISTRIBUTOR(5,1)\|LISTED ITEM(5,1)\|METHANEDIONE GAS(5,1)\|NARROW SPECIES(5,1)\|NUMEROUS NITROGEN SPECIES(5,1)\|REGENERATION REACTION(5,1)\|REMOVING IMPURITY(5,1)\|SINGAPORE CHEMICAL(5,1)\|SOLID MGO RESIDUE(5,1)\|SOLUTION WARMING(5,1)\|TON CO2(5,1)\|UNCONTROLLED FORMATION(5,1)\|HYDROGEN CHLORIDE GAS(4,4)\|5H2O(4,1)\|AERATION(4,1)\|ANHYDROUS MAGNESIUM CHLORIDE(4,1)\|ASCENDING AIR(4,1)\|AUTOHYDROLYSIS DEGREE(4,1)\|AVERAGE SCALE(4,1)\|BLOWER(4,1)\|CLINOPYROXENE(4,1)\|CO2 LOSS(4,1)\|COMPARABLE SOLUTION(4,1)\|COMPLICATION FREE REGENERATION(4,1)\|CONSUMER(4,1)\|CONTAMINANT(4,1)\|CRUSHING(4,1)\|CRYSTALIZATION WATER(4,1)\|DEBACTEROL(4,1)\|DISSOLUTION HEAT(4,1)\|ELEMENT MGO(4,1)\|EXPERIMENT(4,1)\|FERRIC CHLORIDE CONVERSION(4,1)\|FILTRATE(4,1)\|GENUS(4,1)\|GIGATONNE(4,1)\|HEMATITE(4,1)\|HYDROGEN CHLORIDE REGENERATION(4,1)\|HYDROMAGNESITE(4,1)\|INSULATION(4,1)\|INTERMEDIATE SPECIES OXIDATION(4,1)\|IRON CONTENT(4,1)\|JURONG(4,1)\|KINETICS(4,1)\|LEACHING RATE(4,1)\|METAL CHLORIDE HYDROLYSIS(4,1)\|METAL LIBERATION(4,1)\|METALLIC IMPURITY(4,1)\|METHANEDIONE LONG TERM SEQUESTRATION(4,1)\|MG5CA2SI8O(4,1)\|MGO RATIO(4,1)\|MGOHCL(4,1)\|MINERAL CARBONATION(4,1)\|NEGATIVE LIMITATION REMOVING(4,1)\|NH4HCO(4,1)\|NOTATION(4,1)\|\|(US20160319395)\|ULTRAMAFIC ROCK MATERIAL(100,36)\|METAL CARBONATE(100,30)\|AERATE IMPURITY(100,9)\|SALT DECOMPOSITION(89,8)\|PURITY MAGNESITE(73,1)\|ULTRAMAFIC ROCK(54,20)\|AQUEOUS CHESHUNT MIXTURE(54,17)\|PRECIPITATOR(46,8)\|ACID RESIDUE(43,10)\|COEXTRACTION(42,1)\|METHANEDIONE(38,22)\|CHESHUNT MIXTURE(36,20)\|CR OXIDE(36,1)\|METHANEDIONE REACTION(32,2)\|AIR STRIPPER COLUMN(30,19)\|METAL SILICATE(30,8)\|RECYCLING(28,4)\|FURNACE(27,10)\|REACTOR(27,6)\|SALT HYDRATION(27,5)\|ACIDIC VAPOR(26,4)\|PRODUCING METAL CARBONATE(26,4)\|INFRASTRUCTURE(25,3)\|AQUEOUS AMMONIA MOLAR RATIO(24,2)\|ACID LEACHING(24,1)\|METAL OXIDE(21,21)\|VIEWING(20,7)\|METAL PRODUCTION(18,4)\|AMBIENT CONDITION(16,2)\|MAFIC MINERAL(15,3)\|MGCL2 6H2O HYDROLYSIS(14,1)\|GAS LIQUID PACKED COLUMN(13,7)\|ULTRAMAFIC ROCK PARTICLE(13,3)\|MGCL2 6H2O MOLE(13,1)\|PACKED SCRUBBING TOWER(13,1)\|HYDROHALIC ACID(12,3)\|CONCENTRATED SOLUTION(12,2)\|MGCL2 4H2O(12,2)\|CO2 EMISSION MITIGATION(11,1)\|NIO MNO PERCENT(11,1)\|CARBONATION REACTION(10,2)\|HEXAHYDRATE SALT(10,2)\|MAXIMAL DIMENSION(10,2)\|ACCELERATE LIBERATION(10,1)\|AQUEOUS AMMONIA FEASIBILITY(10,1)\|CHANGI WWTP(10,1)\|CO2 MINERALIZATION(10,1)\|DECOMPOSITION THERMODYNAMICS(10,1)\|GASEOUS METHANEDIONE(10,1)\|METAIGNEOUS ROCK(10,1)\|METHANEDIONE CAPTURE(10,1)\|NET CO2 CAPTURE(10,1)\|PACKING RESTRAINER(10,1)\|PASIR PANJANG(10,1)\|PULAU SAKRA(10,1)\|PULAU SERAYA(10,1)\|SINGAPORE OLEFIN(10,1)\|SMPO COGEN(10,1)\|SUBGENERIC GROUPING(10,1)\|VAPOR RECOMPRESSOR(10,1)\|ACID DIGESTION(8,2)\|AMPLE OPPORTUNITY(8,1)\|INDUSTRY INFRASTRUCTURE(8,1)\|LEACHING REQUIREMENT(8,1)\|MGCL2 2H2O(8,1)\|OPERATING COST(8,1)\|SERPENTINE ORE(8,1)\|SIMULTANEOUS EVAPORATION(8,1)\|STRATEGIC IMPORTANCE(8,1)\|MANGANESE(7,7)\|CHROMIUM(7,6)\|THERMOGRAVIMETRIC ANALYSIS(7,4)\|CO2 REMOVAL(7,3)\|COAL GASIFICATION(7,3)\|MG3SI2O(7,3)\|REEMISSION(7,3)\|AMMONIA CAPTURE(7,1)\|AQUEOUS LEACHING(7,1)\|CO2 CAPTURE REACTION(7,1)\|CO2 TON(7,1)\|CONCENTRATED LEACHATE SOLUTION(7,1)\|DIHYDRATE SALT(7,1)\|DIVERSE INDUSTRY(7,1)\|KEEPING ELECTRICITY(7,1)\|LEACHATE SOLUTION PH(7,1)\|LEACHATE STREAM(7,1)\|MG DECOMPOSITION(7,1)\|MGO MOL(7,1)\|MINERALIZATION REACTION(7,1)\|PURIFIED LEACHATE SOLUTION(7,1)\|SATURATED LEACHATE SOLUTION(7,1)\|SLOW DEHYDRATION(7,1)\|T CO2 HR TUA(7,1)\|TANK AGITATION(7,1)\|TETRAHYDRATE SALT(7,1)\|VALUE ADDED METAL SALT(7,1)\|HEATED AIR STRIPPER(6,5)\|11H2O(6,2)\|ALKALINE EARTH SILICATE MINERAL(6,2)\|EVAPORATOR(6,2)\|FIRE RETARDANT(6,2)\|HYDROGEN CHLORIDE STRIPPING(6,2)\|LAND RECLAMATION(6,2)\|METAL REFINERY(6,2)\|NEXT DECADE(6,2)\|NITROUS PRODUCT(6,2)\|HEAVY INDUSTRY(5,4)\|STEAM(5,4)\|HEATING MEDIUM(5,3)\|LEACHING(5,3)\|HSC(5,2)\|CARBONATION PRODUCT(5,1)\|COARSE SILICA SOLID RESIDUE(5,1)\|COMMERCIALIZATION(5,1)\|DESIGNED SCRUBBER(5,1)\|EFFLUENT TREATMENT(5,1)\|ELECTROLYTIC PRODUCTION(5,1)\|ESTABLISHED FUNDAMENTAL(5,1)\|GLOBAL METHANEDIONE LEVEL(5,1)\|GLOBAL SCALE(5,1)\|HARTSHORN(5,1)\|HYDRATED METAL SALT CRYSTALIZATION(5,1)\|INORGANIC SAMPLE(5,1)\|IRON OXIDATION(5,1)\|IRON SEPARATING OXIDE(5,1)\|LEACHING MEDIUM(5,1)\|LIQUID REDISTRIBUTOR(5,1)\|LISTED ITEM(5,1)\|METHANEDIONE GAS(5,1)\|NARROW SPECIES(5,1)\|NUMEROUS NITROGEN SPECIES(5,1)\|REGENERATION REACTION(5,1)\|REMOVING IMPURITY(5,1)\|SINGAPORE CHEMICAL(5,1)\|SOLID MGO RESIDUE(5,1)\|SOLUTION WARMING(5,1)\|TON CO2(5,1)\|UNCONTROLLED FORMATION(5,1)\|HYDROGEN CHLORIDE GAS(4,4)\|5H2O(4,1)\|AERATION(4,1)\|ANHYDROUS MAGNESIUM CHLORIDE(4,1)\|ASCENDING AIR(4,1)\|AUTOHYDROLYSIS DEGREE(4,1)\|AVERAGE SCALE(4,1)\|BLOWER(4,1)\|CLINOPYROXENE(4,1)\|CO2 LOSS(4,1)\|COMPARABLE SOLUTION(4,1)\|COMPLICATION FREE REGENERATION(4,1)\|CONSUMER(4,1)\|CONTAMINANT(4,1)\|CRUSHING(4,1)\|CRYSTALIZATION WATER(4,1)\|DEBACTEROL(4,1)\|DISSOLUTION HEAT(4,1)\|ELEMENT MGO(4,1)\|EXPERIMENT(4,1)\|FERRIC CHLORIDE CONVERSION(4,1)\|FILTRATE(4,1)\|GENUS(4,1)\|GIGATONNE(4,1)\|HEMATITE(4,1)\|HYDROGEN CHLORIDE REGENERATION(4,1)\|HYDROMAGNESITE(4,1)\|INSULATION(4,1)\|INTERMEDIATE SPECIES OXIDATION(4,1)\|IRON CONTENT(4,1)\|JURONG(4,1)\|KINETICS(4,1)\|LEACHING RATE(4,1)\|METAL CHLORIDE HYDROLYSIS(4,1)\|METAL LIBERATION(4,1)\|METALLIC IMPURITY(4,1)\|METHANEDIONE LONG TERM SEQUESTRATION(4,1)\|MG5CA2SI8O(4,1)\|MGCL26H2O(4,1)\|MGO RATIO(4,1)\|MGOHCL(4,1)\|MINERAL CARBONATION(4,1)\|NEGATIVE LIMITATION REMOVING(4,1)\|NH4HCO(4,1)\|NOTATION(4,1)\|\|(WO2015/099612)\|ULTRAMAFIC ROCK MATERIAL(100,28)\|METAL CARBONATE(100,23)\|AERATE IMPURITY(99,8)\|AQUEOUS AMMONIA(81,20)\|SALT DECOMPOSITION(74,6)\|PRECIPITATOR(65,8)\|AQUEOUS CHESHUNT MIXTURE(63,16)\|ULTRAMAFIC ROCK(62,19)\|AQUEOUS AMMONIA MOLAR RATIO(57,2)\|RECYCLING(53,4)\|METHANEDIONE(48,21)\|ACID RESIDUE(43,9)\|METHANEDIONE REACTION(43,3)\|CHESHUNT MIXTURE(42,20)\|MOLAR RATIO(39,6)\|AIR STRIPPER COLUMN(38,19)\|SALT HYDRATION(38,3)\|ACIDIC VAPOR(36,4)\|PACKED COLUMN(34,8)\|METAL SILICATE(32,7)\|FURNACE(31,10)\|PRODUCING METAL CARBONATE(23,3)\|GAS LIQUID PACKED COLUMN(22,7)\|AMBIENT CONDITION(22,2)\|CAO NIO MNOPERCENT(22,1)\|METAL OXIDE(20,18)\|METHANEDIONE MINERALIZATION(20,1)\|ULTRAMAFIC ROCK PARTICLE(18,3)\|PACKED SCRUBBING TOWER(18,1)\|HYDROHALIC ACID(17,3)\|SIMULTANEOUS EVAPORATION(17,2)\|METAL PRODUCTION(16,3)\|COND ITION(16,1)\|DIHYDRATE SALT UNDENVENT(16,1)\|CARBONATION REACTION(14,2)\|HEXAHYDRATE SALT(14,2)\|LIYDRATED SALT(14,2)\|MAXIMAL DIMENSION(14,2)\|ACCELERATE LIBERATION(14,1)\|AQUEOUS AMMONIA FEASIBILITY(14,1)\|COMPRESS EXITINGHCL(14,1)\|DECOMPOSITION THERMODYNAMICS(14,1)\|GASEOUS METHANEDIONE(14,1)\|HANOI WWTP(14,1)\|METHANEDIONE CAPTURE(14,1)\|PACKING RESTRAINER(14,1)\|SUBGENERIC GROUPING(14,1)\|VAPOR RECOMPRESSOR(14,1)\|ACID DIGESTION(13,3)\|AMPLE OPPORTUNITY(12,1)\|EMISSIONPOWER PLANT ENERGY(12,1)\|HR TUA(12,1)\|INDUSTRY INFRASTRUCTURE(12,1)\|LEACHING REQUIREMENT(12,1)\|MGCL HYDROLYSIS(12,1)\|SERPENTINE ORE(12,1)\|STRATEGIC IMPORTANCE(12,1)\|CANY OUT REACTION(11,2)\|MANGANESE(10,7)\|THERMOGRAVIMETRIC ANALYSIS(10,4)\|COAL GASIFICATION(10,3)\|REEMISSION(10,3)\|AMMONIA CAPTURE(10,1)\|AQUEOUS LEACHING(10,1)\|CONCENTRATED LEACHATE SOLUTION(10,1)\|DIVERSE INDUSTRY(10,1)\|HYPOCHLOROUS ACID UNDENVENT(10,1)\|KEEPING ELECTRICITY(10,1)\|LEACHATE SOLUTION PH(10,1)\|LEACHATE STREAM(10,1)\|MG DECOMPOSITION(10,1)\|MGCL2 MOLE(10,1)\|MGO MOL(10,1)\|MINERALIZATION REACTION(10,1)\|PURIFIED LEACHATE SOLUTION(10,1)\|SATURATED LEACHATE SOLUTION(10,1)\|SLOW DEHYDRATION(10,1)\|TANK AGITATION(10,1)\|TETRAHYDRATE SALT(10,1)\|CHROMIUM(9,6)\|HEATED AIR STRIPPER(9,5)\|HEAVY INDUSTRY(8,4)\|STEAM(8,4)\|ALKALINE EARTH SILICATE MINERAL(8,2)\|EVAPORATOR(8,2)\|FIRE RETARDANT(8,2)\|HYDROGEN CHLORIDE STRIPPING(8,2)\|LAND RECLAMATION(8,2)\|METAL REFINERY(8,2)\|NEXT DECADE(8,2)\|NITROUS PRODUCT(8,2)\|CARBONATION PRODUCT(8,1)\|COARSE SILICA SOLID RESIDUE(8,1)\|COMMERCIALIZATION(8,1)\|DESIGNED SCRUBBER(8,1)\|EFFLUENT TREATMENT(8,1)\|ELECTROLYTIC PRODUCTION(8,1)\|ELEMENT MGO SI(8,1)\|ESTABLISHED FUNDAMENTAL(8,1)\|EXCESS WATER CONCURRENT EVAPORATION(8,1)\|GLOBAL METHANEDIONE LEVEL(8,1)\|GLOBAL SCALE(8,1)\|HARTSHORN(8,1)\|HYDRATED METAL SALT CRYSTALIZATION(8,1)\|INORGANIC SAMPLE(8,1)\|IRON OXIDATION(8,1)\|IRON SEPARATING OXIDE(8,1)\|LEACHING MEDIUM(8,1)\|LIQUID REDISTRIBUTOR(8,1)\|LISTED ITEM(8,1)\|MAGNESIUM CHLORIDE HYDROLYSIS(8,1)\|METHANEDIONE GAS(8,1)\|NARROW SPECIES(8,1)\|NUMEROUS NITROGEN SPECIES(8,1)\|REGENERATION REACTION(8,1)\|REMOVING IMPURITY(8,1)\|SOLID MGO RESIDUE(8,1)\|SOLUTION WARMING(8,1)\|UNCONTROLLED FORMATION(8,1)\|HSC(7,2)\|HYDROGEN CHLORIDE GAS(6,4)\|HEATING MEDIUM(6,3)\|LEACHING(6,3)\|MG3SI(6,3)\|ANHYDROUS MAGNESIUM CHLORIDE(6,1)\|ASCENDING AIR(6,1)\|AUTOHYDROLYSIS DEGREE(6,1)\|AVERAGE SCALE(6,1)\|BLOWER(6,1)\|CAPTURE REACTION(6,1)\|CLINOPYROXENE(6,1)\|COMPARABLE SOLUTION(6,1)\|COMPLICATION FREE REGENERATION(6,1)\|CONSUMER(6,1)\|CONTAMINANT(6,1)\|CRUSHING(6,1)\|CRYSTALIZATION WATER(6,1)\|DEBACTEROL(6,1)\|DISSOLUTION HEAT(6,1)\|EMISSION RATE ENERGY(6,1)\|FERRIC CHLORIDE CONVERSION(6,1)\|FILTRATE(6,1)\|GENUS(6,1)\|GIGATONNE(6,1)\|HEMATITE(6,1)\|HYDROGEN CHLORIDE REGENERATION(6,1)\|HYDROMAGNESITE(6,1)\|IGNEOUS ROCK(6,1)\|INSULATION(6,1)\|INTERMEDIATE SPECIES OXIDATION(6,1)\|IRON CONTENT(6,1)\|KINETICS(6,1)\|LEACHING RATE(6,1)\|MAGNESIUMOXIDE(6,1)\|MARKUSH GROUP MEMBER(6,1)\|MERLIMAU(6,1)\|METAL CHLORIDE HYDROLYSIS(6,1)\|METAL LIBERATION(6,1)\|METALLIC IMPURITY(6,1)\|METHANEDIONE LONG TERM SEQUESTRATION(6,1)\|MG5CA2SIS(6,1)\|MGO RATIO(6,1)\|MGOHCL(6,1)\|MINERAL CARBONATION(6,1)\|MITIGATION(6,1)\|NEGATIVE LIMITATION REMOVING(6,1)\|NOTATION(6,1)\|OLIVINE(6,1)\|\|(AU2014370454)\|ULTRAMAFIC ROCK MATERIAL(100,31)\|METAL CARBONATE(100,26)\|AERATE IMPURITY(100,9)\|METAL PRODUCTION(100,3)\|PRODUCING METAL CARBONATE(100,3)\|SALT DECOMPOSITION(75,7)\|ULTRAMAFIC ROCK(54,20)\|AQUEOUS CHESHUNT MIXTURE(54,17)\|PRECIPITATOR(46,8)\|ACID RESIDUE(43,10)\|CHESHUNT MIXTURE(36,21)\|METAL SILICATE(30,8)\|METHANEDIONE REACTION(30,3)\|RECYCLING(28,4)\|FURNACE(27,10)\|REACTOR(27,6)\|SALT HYDRATION(27,5)\|AIR STRIPPER COLUMN(26,18)\|ACIDIC VAPOR(26,4)\|AQUEOUS AMMONIA MOLAR RATIO(24,2)\|METAL OXIDE(19,20)\|COGEN PASIR PANJANG(18,1)\|PULAU SAKRA SINGAPORE(18,1)\|PACKED COLUMN LIQUID(17,1)\|PULAU I1ERLIMAU ISLAND(17,1)\|AMBIENT CONDITION(16,2)\|GAS LIQUID PACKED COLUMN(15,7)\|METHANEDIONE MINERALIZATION(14,1)\|MGCL2 6H2O HYDROLYSIS(14,1)\|ULTRAMAFIC ROCK PARTICLE(13,3)\|PACKED SCRUBBING TOWER(13,1)\|HYDROHALIC ACID(12,3)\|HCI MOLE(12,2)\|HCI STRIPPING(12,2)\|CO2 EMISSION MITIGATION(11,1)\|ACID DIGESTION(10,3)\|CARBONATION REACTION(10,2)\|HEXAHYDRATE SALT(10,2)\|MAXIMAL DIMENSION(10,2)\|ACCELERATE LIBERATION(10,1)\|AQUEOUS AMMONIA FEASIBILITY(10,1)\|CO2 MINERALIZATION(10,1)\|DECOMPOSING MGC(10,1)\|DECOMPOSITION THERMODYNAMICS(10,1)\|GASEOUS METHANEDIONE(10,1)\|METAIGNEOUS ROCK(10,1)\|METHANEDIONE CAPTURE(10,1)\|NET CO2 CAPTURE(10,1)\|PACKING RESTRAINER(10,1)\|SINGAPORE OLEFIN(10,1)\|SUBGENERIC GROUPING(10,1)\|VAPOR RECOMPRESSOR(10,1)\|AMPLE OPPORTUNITY(8,1)\|ANHYDROUS MGC(8,1)\|CO2 ERNISSION ENERGY(8,1)\|INDUSTRY INFRASTRUCTURE(8,1)\|LEACHING REQUIREMENT(8,1)\|MOLTEN MGC(8,1)\|REMAINING UNREACTED HCI(8,1)\|SATURATED MGC(8,1)\|SERPENTINE ORE(8,1)\|SIMULTANEOUS EVAPORATION(8,1)\|STRATEGIC IMPORTANCE(8,1)\|MANGANESE(7,7)\|CHROMIUM(7,6)\|CO2 REMOVAL(7,3)\|COAL GASIFICATION(7,3)\|REEMISSION(7,3)\|AMMONIA CAPTURE(7,1)\|AQUEOUS LEACHING(7,1)\|CATION EXTRACTION(7,1)\|CO2 CAPTURE REACTION(7,1)\|CO2 TON(7,1)\|CONCENTRATED LEACHATE SOLUTION(7,1)\|DIHYDRATE SALT(7,1)\|DIVERSE INDUSTRY(7,1)\|FEC CONVERSION(7,1)\|KEEPING ELECTRICITY(7,1)\|LEACHATE SOLUTION PH(7,1)\|LEACHATE STREAM(7,1)\|MG DECOMPOSITION(7,1)\|MGC MOLE(7,1)\|MGO MOL(7,1)\|MINERALIZATION REACTION(7,1)\|PURIFIED LEACHATE SOLUTION(7,1)\|SATURATED LEACHATE SOLUTION(7,1)\|SLOW DEHYDRATION(7,1)\|TANK AGITATION(7,1)\|TETRAHYDRATE SALT(7,1)\|HEATED AIR STRIPPER(6,5)\|ALKALINE EARTH SILICATE MINERAL(6,2)\|EVAPORATOR(6,2)\|FIRE RETARDANT(6,2)\|LAND RECLAMATION(6,2)\|METAL REFINERY(6,2)\|NEXT DECADE(6,2)\|NITROUS PRODUCT(6,2)\|HEAVY INDUSTRY(5,4)\|STEAM(5,4)\|EXCESS WATER(5,3)\|FERRIC CHLORIDE(5,3)\|HEATING MEDIUM(5,3)\|LEACHING(5,3)\|THERMOGRAVIMETRIC ANALYSIS(5,3)\|HSC(5,2)\|CARBONATION PRODUCT(5,1)\|CO2 EMISSION RATE(5,1)\|COARSE SILICA SOLID RESIDUE(5,1)\|COMMERCIALIZATION(5,1)\|DESIGNED SCRUBBER(5,1)\|EFFLUENT TREATMENT(5,1)\|ELECTROLYTIC PRODUCTION(5,1)\|ENERGY CO2 EMISSION(5,1)\|ESTABLISHED FUNDAMENTAL(5,1)\|GLOBAL METHANEDIONE LEVEL(5,1)\|GLOBAL SCALE(5,1)\|H2O FE(5,1)\|HARTSHORN(5,1)\|HYDRATED METAL SALT CRYSTALIZATION(5,1)\|INORGANIC SAMPLE(5,1)\|IRON OXIDATION(5,1)\|IRON SEPARATING OXIDE(5,1)\|LEACHING MEDIUM(5,1)\|LIQUID REDISTRIBUTOR(5,1)\|LISTED ITEM(5,1)\|MAGNESIUM CHLORIDE HEXAHYDRATE HYDROLYSIS(5,1)\|METHANEDIONE GAS(5,1)\|NARROW SPECIES(5,1)\|NUMEROUS NITROGEN SPECIES(5,1)\|REGENERATION REACTION(5,1)\|REMOVING IMPURITY(5,1)\|SOLID MGO RESIDUE(5,1)\|SOLUTION WARMING(5,1)\|TON CO2(5,1)\|UNCONTROLLED FORMATION(5,1)\|AERATION(4,1)\|ASCENDING AIR(4,1)\|AUTOHYDROLYSIS DEGREE(4,1)\|AVERAGE SCALE(4,1)\|BLOWER(4,1)\|CLINOPYROXENE(4,1)\|CO2 LOSS(4,1)\|COMPARABLE SOLUTION(4,1)\|COMPLICATION FREE REGENERATION(4,1)\|CONSUMER(4,1)\|CONTAMINANT(4,1)\|CRUSHING(4,1)\|CRYSTALIZATION WATER(4,1)\|DEBACTEROL(4,1)\|DISSOLUTION HEAT(4,1)\|FILTRATE(4,1)\|GENUS(4,1)\|GIGATONNE(4,1)\|HEMATITE(4,1)\|HYDROMAGNESITE(4,1)\|INSULATION(4,1)\|INTERMEDIATE SPECIES OXIDATION(4,1)\|IRON CONTENT(4,1)\|KINETICS(4,1)\|LEACHING RATE(4,1)\|METAL CHLORIDE HYDROLYSIS(4,1)\|METAL LIBERATION(4,1)\|METALLIC IMPURITY(4,1)\|METHANEDIONE LONG TERM SEQUESTRATION(4,1)\|MG3SI2O(4,1)\|MG5CA2SI(4,1)\|MGO RATIO(4,1)\|MINERAL CARBONATION(4,1)\|NEGATIVE LIMITATION REMOVING(4,1)\|NH4HCO(4,1)\|NOTATION(4,1)\|OLIVINE(4,1)\|\|(AU2014370454)\|ULTRAMAFIC ROCK MATERIAL(100,31)\|METAL CARBONATE(100,26)\|AERATE IMPURITY(100,9)\|METAL PRODUCTION(100,3)\|PRODUCING METAL CARBONATE(100,3)\|SALT DECOMPOSITION(75,7)\|ULTRAMAFIC ROCK(54,20)\|AQUEOUS CHESHUNT MIXTURE(54,17)\|PRECIPITATOR(46,8)\|ACID RESIDUE(43,10)\|CHESHUNT MIXTURE(36,21)\|METAL SILICATE(30,8)\|METHANEDIONE REACTION(30,3)\|RECYCLING(28,4)\|FURNACE(27,10)\|REACTOR(27,6)\|SALT HYDRATION(27,5)\|AIR STRIPPER COLUMN(26,18)\|ACIDIC VAPOR(26,4)\|AQUEOUS AMMONIA MOLAR RATIO(24,2)\|METAL OXIDE(19,20)\|COGEN PASIR PANJANG(18,1)\|PULAU SAKRA SINGAPORE(18,1)\|PACKED COLUMN LIQUID(17,1)\|PULAU I1ERLIMAU ISLAND(17,1)\|AMBIENT CONDITION(16,2)\|GAS LIQUID PACKED COLUMN(15,7)\|METHANEDIONE MINERALIZATION(14,1)\|MGCL2 6H2O HYDROLYSIS(14,1)\|ULTRAMAFIC ROCK PARTICLE(13,3)\|PACKED SCRUBBING TOWER(13,1)\|HYDROHALIC ACID(12,3)\|HCI MOLE(12,2)\|HCI STRIPPING(12,2)\|CO2 EMISSION MITIGATION(11,1)\|ACID DIGESTION(10,3)\|CARBONATION REACTION(10,2)\|HEXAHYDRATE SALT(10,2)\|MAXIMAL DIMENSION(10,2)\|ACCELERATE LIBERATION(10,1)\|AQUEOUS AMMONIA FEASIBILITY(10,1)\|CO2 MINERALIZATION(10,1)\|DECOMPOSING MGC(10,1)\|DECOMPOSITION THERMODYNAMICS(10,1)\|GASEOUS METHANEDIONE(10,1)\|METAIGNEOUS ROCK(10,1)\|METHANEDIONE CAPTURE(10,1)\|NET CO2 CAPTURE(10,1)\|PACKING RESTRAINER(10,1)\|SINGAPORE OLEFIN(10,1)\|SUBGENERIC GROUPING(10,1)\|VAPOR RECOMPRESSOR(10,1)\|AMPLE OPPORTUNITY(8,1)\|ANHYDROUS MGC(8,1)\|CO2 ERNISSION ENERGY(8,1)\|INDUSTRY INFRASTRUCTURE(8,1)\|LEACHING REQUIREMENT(8,1)\|MOLTEN MGC(8,1)\|REMAINING UNREACTED HCI(8,1)\|SATURATED MGC(8,1)\|SERPENTINE ORE(8,1)\|SIMULTANEOUS EVAPORATION(8,1)\|STRATEGIC IMPORTANCE(8,1)\|MANGANESE(7,7)\|CHROMIUM(7,6)\|CO2 REMOVAL(7,3)\|COAL GASIFICATION(7,3)\|REEMISSION(7,3)\|AMMONIA CAPTURE(7,1)\|AQUEOUS LEACHING(7,1)\|CATION EXTRACTION(7,1)\|CO2 CAPTURE REACTION(7,1)\|CO2 TON(7,1)\|CONCENTRATED LEACHATE SOLUTION(7,1)\|DIHYDRATE SALT(7,1)\|DIVERSE INDUSTRY(7,1)\|FEC CONVERSION(7,1)\|KEEPING ELECTRICITY(7,1)\|LEACHATE SOLUTION PH(7,1)\|LEACHATE STREAM(7,1)\|MG DECOMPOSITION(7,1)\|MGC MOLE(7,1)\|MGO MOL(7,1)\|MINERALIZATION REACTION(7,1)\|PURIFIED LEACHATE SOLUTION(7,1)\|SATURATED LEACHATE SOLUTION(7,1)\|SLOW DEHYDRATION(7,1)\|TANK AGITATION(7,1)\|TETRAHYDRATE SALT(7,1)\|HEATED AIR STRIPPER(6,5)\|ALKALINE EARTH SILICATE MINERAL(6,2)\|EVAPORATOR(6,2)\|FIRE RETARDANT(6,2)\|LAND RECLAMATION(6,2)\|METAL REFINERY(6,2)\|NEXT DECADE(6,2)\|NITROUS PRODUCT(6,2)\|HEAVY INDUSTRY(5,4)\|STEAM(5,4)\|EXCESS WATER(5,3)\|FERRIC CHLORIDE(5,3)\|HEATING MEDIUM(5,3)\|LEACHING(5,3)\|THERMOGRAVIMETRIC ANALYSIS(5,3)\|HSC(5,2)\|CARBONATION PRODUCT(5,1)\|CO2 EMISSION RATE(5,1)\|COARSE SILICA SOLID RESIDUE(5,1)\|COMMERCIALIZATION(5,1)\|DESIGNED SCRUBBER(5,1)\|EFFLUENT TREATMENT(5,1)\|ELECTROLYTIC PRODUCTION(5,1)\|ENERGY CO2 EMISSION(5,1)\|ESTABLISHED FUNDAMENTAL(5,1)\|GLOBAL METHANEDIONE LEVEL(5,1)\|GLOBAL SCALE(5,1)\|H2O FE(5,1)\|HARTSHORN(5,1)\|HYDRATED METAL SALT CRYSTALIZATION(5,1)\|INORGANIC SAMPLE(5,1)\|IRON OXIDATION(5,1)\|IRON SEPARATING OXIDE(5,1)\|LEACHING MEDIUM(5,1)\|LIQUID REDISTRIBUTOR(5,1)\|LISTED ITEM(5,1)\|MAGNESIUM CHLORIDE HEXAHYDRATE HYDROLYSIS(5,1)\|METHANEDIONE GAS(5,1)\|NARROW SPECIES(5,1)\|NUMEROUS NITROGEN SPECIES(5,1)\|REGENERATION REACTION(5,1)\|REMOVING IMPURITY(5,1)\|SOLID MGO RESIDUE(5,1)\|SOLUTION WARMING(5,1)\|TON CO2(5,1)\|UNCONTROLLED FORMATION(5,1)\|AERATION(4,1)\|ASCENDING AIR(4,1)\|AUTOHYDROLYSIS DEGREE(4,1)\|AVERAGE SCALE(4,1)\|BLOWER(4,1)\|CLINOPYROXENE(4,1)\|CO2 LOSS(4,1)\|COMPARABLE SOLUTION(4,1)\|COMPLICATION FREE REGENERATION(4,1)\|CONSUMER(4,1)\|CONTAMINANT(4,1)\|CRUSHING(4,1)\|CRYSTALIZATION WATER(4,1)\|DEBACTEROL(4,1)\|DISSOLUTION HEAT(4,1)\|FILTRATE(4,1)\|GENUS(4,1)\|GIGATONNE(4,1)\|HEMATITE(4,1)\|HYDROMAGNESITE(4,1)\|INSULATION(4,1)\|INTERMEDIATE SPECIES OXIDATION(4,1)\|IRON CONTENT(4,1)\|KINETICS(4,1)\|LEACHING RATE(4,1)\|METAL CHLORIDE HYDROLYSIS(4,1)\|METAL LIBERATION(4,1)\|METALLIC IMPURITY(4,1)\|METHANEDIONE LONG TERM SEQUESTRATION(4,1)\|MG3SI2O(4,1)\|MG5CA2SI(4,1)\|MGO RATIO(4,1)\|MINERAL CARBONATION(4,1)\|NEGATIVE LIMITATION REMOVING(4,1)\|NH4HCO(4,1)\|NOTATION(4,1)\|OLIVINE(4,1)\|	(US9896741)\|The invention claimed is:\|1. A method of producing a metal carbonate from an ultramafic rock material, the method comprising\| a) providing an ultramafic rock material comprising a metal silicate;\| b) reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| c) contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| d) heating the resultant mixture from step c) to decompose the salt of the metal to form metal oxide; and\| e) reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|2. The method according to claim 1, wherein molar ratio of metal to CO3 in the metal carbonate is in the range of about 1:1 to about 5:4.\|3. The method according to claim 1, wherein the metal carbonate is magnesium carbonate.\|4. The method according to claim 1, wherein the ultramafic rock material comprises serpentine.\|5. The method according to claim 1, wherein the acid is a hydrohalic acid.\|6. The method according to claim 1, wherein the acid comprises hydrochloric acid.\|7. The method according to claim 6, wherein concentration of the hydrochloric acid is at least 27 wt % HCl.\|8. The method according to claim 1, wherein reacting the ultramafic rock material with an acid is carried out at a temperature in the range of about 80° C. to about 100° C.\|9. The method according to claim 1, wherein contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature in the range of about 150° C. to about 250° C.\|10. The method according to claim 1, wherein contacting the mixture comprising a salt of the metal with oxygen is carried out under conditions such that pH of the mixture is less than or equal to 9.\|11. The method according to claim 1, wherein contacting the mixture comprising a salt of the metal with oxygen is carried out for a time period suitable to form a mixture saturated with the salt.\|12. The method according to claim 1, further comprising removing water from the resultant mixture from step c) prior to step d) to form a hydrated salt of the metal.\|13. The method according to claim 1, wherein reacting the metal oxide with aqueous ammonium carbonate is carried out at ambient conditions.\|14. The method according to claim 1, wherein the aqueous ammonium carbonate is obtained by reacting carbon dioxide with aqueous ammonia in a gas-liquid packed column.\|15. The method according to claim 14, wherein molar ratio of aqueous ammonia to carbon dioxide is in the range of about 2:1 to about 2.5:1.\|16. A system for producing a metal carbonate from ultramafic rock material, the system comprising\| a) a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| b) an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| c) a furnace configured to heat the resultant mixture from step b) to decompose the salt of the metal to form the metal oxide; and\| d) a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|17. The system according to claim 16, further comprising a gas-liquid packed column arranged upstream of the precipitator and configured to carry out reaction of carbon dioxide with aqueous ammonia to form aqueous ammonium carbonate.\|18. The system according to claim 17, further comprising recycling means configured to recycle aqueous ammonia from the precipitator to the gas-liquid packed column.\|19. The system according to claim 16, further comprising a compressor configured to compress acid vapor and/or water vapor from the air stripper column.\|20. The system according to claim 16, further comprising recycling means configured to recycle acid vapor and/or water vapor from the air stripper column and/or the furnace to the reactor and/or the air stripper column.	(US9896741)\|TECHNICAL FIELD\|[0002] The invention relates to methods of producing metal carbonate from an ultramafic rock material.\|BACKGROUND\|[0003] Heavy industries such as steel making, coal gasification, metal refineries, power plants and cement making units emit a significant amount of carbon dioxide (CO2). Taking Singapore, for example, it was estimated that amount of carbon dioxide from power plants will exceed 20 million tonnes per year for the next decade (see TABLE 1).\|[0004] TABLE 1 Carbon dioxide (CO2) emissions from power plants in Singapore (2007-2017) 2007 Energy and CO2 Emission2017 Energy and CO2 Emission CO2Emission CO2Emission EnergyEmissionrateEnergyEmissionratePower PlantMWh/aMt CO2/at CO2/hrMWh/aMt CO2/at CO2/hr TUAS8,867,2754.0045717,100,00013.201507PULAU SERAYA8,297,8683.9344813,000,0006.00685SENOKO11,200,0004.4550811,500,0004.56520PULAU MERLIMAU0 2,931,1241.29147ISLAND POWER0 2,537,8751.27145PULAU SAKRA2,090,1030.871002,177,4970.91104SINGAPORE CHEMICAL684,5770.38431,610,5930.8395JURONG325,7140.1518363,8600.1719SINGAPORE OLEFINS318,4060.1517332,2270.1618CHANGI WWTP257,3030.1214276,9990.1315SMPO COGEN173,3210.1112182,3920.1113PASIR PANJANG185,0810.0910200,6640.1011Total32,399,64814.3 52,213,23028.7 Source: http://carma.org/region/detail/169\|[0005] Carbon dioxide capture and storage by mineralization has been proposed as a possible technology to reduce global carbon dioxide levels. The technology may include extracting cations from feed material such as rocks, and combining the cations with carbon dioxide to form a stable carbonate material. Due to the large quantities (gigatonnes) of material involved, ability to extract metal from the feed material at high efficiencies is important. Limitations to existing processes include low metal extraction yields and high energy consumption, due to removal of water which has high latent and sensible heat.\|[0006] In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|SUMMARY\|[0007] In a first aspect, a method of producing a metal carbonate from an ultramafic rock material is provided. The method comprises\| - a) providing an ultramafic rock material comprising a metal silicate;\| - b) reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| - c) contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| - d) heating the resultant mixture from step c) to decompose the salt of the metal to form metal oxide; and\| - e) reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|[0013] In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided. The system comprises\| - a) a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| - b) an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| - c) a furnace configured to heat the resultant mixture from step b) to decompose the salt of the metal to form the metal oxide; and\| - d) a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to form the metal carbonate.\|(US9896741)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] The invention will be better understood with reference to the detailed description when considered in conjunction with the non-limiting examples and the accompanying drawings, in which:\|[0019] FIG. 1 is a schematic diagram depicting working mechanism of an air stripper column. Notations in the figures represent the following: 101: packed column; 102: packing material; 103: packing support; 104: packing restrainer; 105: liquid redistributors; 106: blower assembly; 111: contaminant influent; 112: spray; 113: air in; 114: gas out to atmosphere or secondary treatment; and 115: treated effluent.\|[0020] FIG. 2 is a schematic diagram showing process flow for a mineralization process according to an embodiment.\|[0021] FIG. 3 is a graph showing thermogravimetric analysis (TGA) results of MgCl2.6H2O. Y-axis: weight; x-axis: temperature (° C.).\|[0022] FIG. 4 is a graph showing TGA analysis of magnesium carbonate product from reaction of MgO with (NH4)2CO3. Y-axis: weight (mg); x-axis: temperature (° C.).\|[0023] FIG. 5 is a schematic diagram showing general process flow for a system to carry out mineralization process according to embodiments.\|(US9896741)\|DETAILED DESCRIPTION\|[0024] Using methods disclosed herein, carbon dioxide emitted from various sources, such as coal gasification and power plants, may be captured in the form of metal carbonates such as magnesium carbonate, without significant modification of existing infrastructure. The metal carbonates are thermodynamically stable and inert, and once bound, the carbon dioxide that is captured is not susceptible to re-emission into the atmosphere. Furthermore, the metal carbonates produced may be in solid form to render their ease of handling.\|[0025] Various embodiments disclosed herein are particularly suited for long-term sequestration of carbon dioxide emitted from industries. Advantageously, systems for producing metal carbonate disclosed herein may be integrated into existing infrastructure of industries so as to utilize waste heat from the industries in production of metal carbonates. The metal carbonates produced may be used as building materials or for land reclamation purposes, or be used as additives for adding to polymers as fire retardants.\|[0026] With the above in mind, various embodiments refer in a first aspect to a method of producing a metal carbonate from an ultramafic rock material.\|[0027] The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|[0028] As used herein, the term “ultramafic rock material” refers to igneous and meta-igneous rocks which are composed of more than 90% mafic minerals in various proportions with trace amounts of other minerals. The term “mafic” is used to describe a silicate mineral or rock that is rich in magnesium. Apart from magnesium, the ultramafic rock material may also contain metals such as iron, nickel, chromium, manganese and/or calcium as impurities.\|[0029] Main mafic minerals include olivine (Mg2SiO4), orthopyroxene (MgSiO3), and clinopyroxene ((MgCa)SiO3). Upon hydration, the corresponding mafic minerals are serpentine (Mg3Si2O5(OH)4), tremolite (Mg5Ca2Si8O22(OH)2), and talc (Mg3Si4O10(OH)2).\|[0030] Of particular importance is serpentine, as it is volumetrically dominant on a global scale. Typically, serpentine has a silica content of less than 45%, magnesium oxide content of greater than 18%, and a high iron oxide content in the range of about 5% to 15%. Content of serpentine may vary between the stated ranges depending on source and quality of the rock. TABLE 2 depicts composition of serpentine according to an embodiment. The values are obtained from direct measurements of the mineral samples using X-ray fluorescence spectroscopy.\|[0031] TABLE 2 Composition of Serpentine (Percentage expressed in terms of weight% of the respective oxides contained within the material)ElementMgOSiO2Fe2O3Al2O3Cr2O3CaONiOMnO Percent46.7242.78.40.610.450.40.290.14 \|[0032] In various embodiments, the ultramafic rock material comprises or consists of serpentine.\|[0033] As mentioned above, the ultramafic rock material is rich in magnesium. Accordingly, in various embodiments, the method of producing metal carbonate from an ultramafic rock material is used to produce magnesium carbonate. Molar ratio of metal to carbonate (CO3) in the metal carbonate may be in the range of about 1:1 to about 5:4. In various embodiments, molar ratio of metal to CO3 in the metal carbonate is about 1:1.\|[0034] The method includes providing an ultramafic rock material comprising a metal silicate. In various embodiments, the metal silicate is magnesium silicate, such as Mg3Si2O5(OH)4. Apart from magnesium silicate, silicates of other metals contained in the ultramafic rock material may also be present, such as silicates of iron, nickel, chromium, manganese, and/or calcium.\|[0035] Providing an ultramafic rock material comprising a metal silicate may include physically working the ultramafic rock material such as by crushing or grinding, so as to reduce size of the ultramafic rock material. Advantageously, by reducing size of the ultramafic rock material, liberation of metal from the ultramafic rock material may be accelerated.\|[0036] In some embodiments, providing an ultramafic rock material includes physically working the ultramafic rock material to form ultramafic rock particles having a size of 0.5 mm or less. Size of the ultramafic rock particles may be characterized by its maximal dimension, wherein the term “maximal dimension” refers to the maximal length of a straight line segment passing through the center of a figure and terminating at the periphery.\|[0037] For example, the ultramafic rock material may comprise or consist of ultramafic rock particles having a size of 0.5 mm or less, such as a size in the range of about 0.01 mm to about 0.5 mm, about 0.05 mm to about 0.5 mm, about 0.1 mm to about 0.5 mm, about 0.2 mm to about 0.5 mm, about 0.01 mm to about 0.3 mm, about 0.01 mm to about 0.1 mm, or about 0.1 mm to about 0.3 mm.\|[0038] The method includes reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal. In reacting the ultramafic rock material with an acid, metal from the ultramafic rock material may be leached out in the form of a metal salt. Hence, the mixture containing the salt of the metal may otherwise be termed as the leachate. A solid residue of coarse silica may also be obtained following reacting of the ultramafic rock material with acid.\|[0039] The acid may, for example, be selected from the group consisting of hydrohalic acid, sulfuric acid (H2SO4), nitric acid (HNO3), phosphoric acid (H3PO4), acetic acid (CH3COOH), and combinations thereof. Depending on the acid used, different metal salts may be formed. For example, salt of the metal may be a halide such as a chloride or a bromide, a sulfate, a nitrate, a phosphate, and/or an acetate. In various embodiments, the acid is a hydrohalic acid, such as hydrofluoric acid (HF), hydrochloric acid (HCl), hydrobromic acid (HBr), and/or hydroiodic acid (HI). In some embodiments, the acid comprises or consists of hydrochloric acid and/or hydrobromic acid.\|[0040] In specific embodiments, the acid comprises or consists of hydrochloric acid. By reacting the ultramafic rock material with hydrochloric acid, metal may be leached from the ultramafic rock material as metal chloride. Use of hydrochloric acid has been found by the inventors to be advantageous, as hydrochloric acid is able to leach metal effectively from ultramafic rock material, and may be regenerated easily and simply without complication. Undesirable decompositions do not take place upon heating of metal chlorides, as opposed to the case of metal nitrates formed from reacting metal silicates with nitric acid, for example, which may generate nitrite and nitrous products.\|[0041] The mixture may accordingly contain chlorides of magnesium, iron, nickel, chromium, manganese, and/or calcium. Due to the high magnesium content in ultramafic rock material, the salt of the metal may mainly be made up of magnesium chloride.\|[0042] In various embodiments, concentration of the hydrochloric acid is at least 27 wt % HCl. For example, concentration of the hydrochloric acid may be at least 30 wt %, at least 35 wt % HCl, or be in the range of about 27 wt % to about 35 wt %, about 27 wt % to about 32 wt %, or about 27 wt % to about 30 wt % HCl.\|[0043] Reacting the ultramafic rock material with an acid may be carried out at a temperature in the range of about 80° C. to about 100° C. For example, reacting the ultramafic rock material with an acid may be carried out at a temperature in the range of about 80° C. to about 95° C., about 80° C. to about 90° C., about 80° C. to about 85° C., about 90° C. to about 100° C., or about 85° C. to about 95° C. In various embodiments, reacting the ultramafic rock material with an acid is carried out under continuous stirring to accelerate liberation of metal from the ultramafic rock material.\|[0044] The method includes contacting the mixture comprising a salt from the metal with oxygen. The oxygen may be in the form of an oxygen flow and/or an air flow. This may be carried out to aerate impurities in the mixture and/or to remove residual acid from the mixture. As mentioned above, the ultramafic rock material may also contain metals such as iron, nickel, chromium, manganese and/or calcium as impurities. By contacting the mixture comprising a salt of the metal with oxygen, the metals may be aerated to their respective oxides and may be precipitated out from the mixture to allow their removal from the resultant mixture by a separation process such as decanting or filtering.\|[0045] By way of example only, this aeration process may be illustrated using hydrochloric acid and iron. Iron may be leached from ultramafic rock material using hydrochloric acid to form iron (II) chloride (FeCl2). The iron (II) chloride may be oxidized readily to iron (III) chloride (FeCl3) upon contact with oxygen, as shown in equation (1):\|12FeCl2+3O2→2Fe2O3+8FeCl3 (1)\|[0046] The iron (III) chloride may undergo auto-hydrolysis in solution to form iron (III) oxide and hydrogen chloride, as shown in equation (2):\|2FeCl3+3H2O→Fe2O3+6HCl (2)\|[0047] Iron (III) oxide may be precipitated out from the mixture following oxidation to allow their easy removal.\|[0048] In various embodiments, contacting the mixture comprising a salt of the metal with oxygen to aerate impurities in the mixture comprises separating oxides of iron, nickel, chromium, aluminum and/or manganese from the resultant mixture following oxidation.\|[0049] Further, from equation (2), it may be seen that by eliminating hydrochloric acid from the solution, conversion of iron (III) chloride into iron (III) oxide may be promoted. This means that metal impurities in the mixture may be removed to a greater extent by removing hydrochloric acid from the mixture. Advantageously, the removal of hydrochloric acid, which may arise from the auto-hydrolysis process as well as residual acid present in the mixture, may be carried out by contacting the mixture comprising a salt of the metal with oxygen.\|[0050] Contacting the mixture comprising a salt of the metal with oxygen may be carried out in a flow of air and/or oxygen. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out by air stripping. As used herein, the term “air stripping” refers to a process by which an air stream is used to remove dissolved gases or volatile components of a liquid. The air stripping may be carried out in an air stripper column. For example, the mixture comprising a salt of the metal may be introduced at the top of an air stripper column. The air stripper column may contain packing material to provide a larger contact surface area for aeration. Air may be introduced at the bottom of the air stripper column, such that the mixture flows in opposite direction to the ascending air while contacting each other. In so doing, the air may strip acid from the mixture. The air exits from the top of the air stripper column, while the resultant mixture, which has been at least partially stripped of acid, may leave the bottom of the air stripper column for channeling into a subsequent stage.\|[0051] In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out under conditions such that pH of the mixture is less than or equal to 9. For example, the contacting may be carried out under conditions such that pH of the mixture is in the range of about 3 to about 9, about 5 to about 9, about 7 to about 9, about 3 to about 7, about 3 to about 5, about 5 to about 7, or about 4 to about 6.\|[0052] Contacting the mixture comprising a salt of the metal with oxygen may be carried out at a temperature in the range of about 150° C. to about 250° C., such as about 180° C. to about 250° C., about 200° C. to about 250° C., about 150° C. to about 220° C., about 150° C. to about 200° C., about 180° C. to about 220° C., or about 180° C. to about 200° C. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature in the range of about 180° C. to about 200° C. In some embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature of about 200° C.\|[0053] By contacting the mixture comprising a salt of the metal with oxygen at elevated temperatures, water may be evaporated or vaporized from the mixture to form steam. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out for a time period suitable to form a mixture saturated with the salt. Advantageously, by removing water from the mixture, this minimizes water content in the mixture for removal in a subsequent stage. At the same time, heat energy may be recovered in the form of steam for rechanneling back into the process.\|[0054] By removing water from the mixture, a hydrated salt of the metal may also be formed. In various embodiments, the hydrated salt of the metal comprises or consists essentially of magnesium chloride hydrates. Water of crystallization of the hydrated metal salt may be in the range of about 2 to about 6, such as 2, 3, 4, 5, or 6.\|[0055] The method of the first aspect includes heating the resultant mixture following contact with oxygen to decompose the salt of the metal to form metal oxide. For example, the metal oxide may contain magnesium oxide, along with trace amounts of oxides of iron, nickel, chromium, manganese, and/or calcium which may not have been removed in an earlier stage.\|[0056] In various embodiments, heating the resultant mixture is carried out at a temperature in the range of about 400° C. to about 600° C., such as about 450° C. to about 600° C., about 500° C. to about 600° C., about 550° C. to about 600° C., about 400° C. to about 550° C., or about 450° C. to about 550° C. In specific embodiments, heating the resultant mixture is carried out at a temperature of about 550° C.\|[0057] Given the high temperatures, steam may be generated. In embodiments where the acid is hydrochloric acid, and where residual acid is present in the resultant mixture not removed in an earlier stage, hydrogen chloride gas may additionally be produced.\|[0058] The metal oxide is reacted with aqueous ammonium carbonate to obtain the metal carbonate. At the same time, aqueous ammonia may be produced.\|[0059] The aqueous ammonium carbonate may be obtained by reacting carbon dioxide with aqueous ammonia, which may be carried out in a gas-liquid packed column. The carbon dioxide may be comprised in a flue gas, which may be channeled from heavy industries such as a power plant.\|[0060] Molar ratio of aqueous ammonia to carbon dioxide may be in the range of about 2:1 to about 2.5:1, such as about 2.1:1, 2.2:1, 2.3:1, 2,4:1, or about 2.5:1.\|[0061] In various embodiments, reacting carbon dioxide with aqueous ammonia is carried out at a pH of at least 9 to maximize degree of carbonation. For example, reacting carbon dioxide with aqueous ammonia may be carried out at a pH in the range of about 9 to about 13, about 9 to about 12, about 9 to about 11, about 9 to about 10, about 10 to about 13, about 11 to about 13, or about 10 to about 12. In some embodiments, reacting carbon dioxide with aqueous ammonia is carried out at a pH of at least 10.\|[0062] Advantageously, reacting the metal oxide with aqueous ammonium carbonate may be carried out at ambient conditions.\|[0063] In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided. The system comprises a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal; an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen to aerate impurities in the mixture and/or to remove residual acid from the mixture; a furnace configured to heat the resultant mixture to decompose the salt of the metal to form the metal oxide; and a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. Schematic diagram of a system for producing a metal carbonate from ultramafic rock material according to embodiments is shown in FIG. 5 and discussed in Example 8. Processing conditions for operating the various components of the system have already been discussed above.\|[0064] In various embodiments, the system further comprises a gas-liquid packed column arranged upstream of the precipitator and configured to carry out reaction of carbon dioxide with aqueous ammonia to form aqueous ammonium carbonate. As mentioned above, the carbon dioxide may be comprised in a flue gas, which may be channeled from heavy industries such as a power plant. The ammonium carbonate that is formed may be used to react with the metal oxide to form metal carbonate. In so doing, carbon dioxide may be captured in the metal carbonate which is thermodynamically stable and inert, thereby rendering the carbon dioxide that is captured not susceptible for re-emission into the atmosphere.\|[0065] The system may further comprise a compressor configured to compress acid vapor and/or water vapor from the air stripper column. This allows formation of higher quality steam that may be used to supplement heating medium that may be used for operating the air stripper column.\|[0066] The system may, in various embodiments, comprise recycling means configured to recycle acid vapor and/or water vapor from the air stripper column and/or the furnace to the reactor and/or the air stripper column. In so doing, heat energy that is generated from the air stripper column and/or the furnace may be reused in other parts of the process, thereby minimizing energy consumption of the system.\|[0067] In various embodiments, the system further comprises recycling means configured to recycle aqueous ammonia from the precipitator to the gas-liquid packed column. As mentioned above, metal oxide may be reacted with aqueous ammonium carbonate to obtain metal carbonate in the precipitator, while producing aqueous ammonia at the same time. By recycling the aqueous ammonia produced to the gas-liquid packed column, the aqueous ammonia may be reused to react with carbon dioxide to form aqueous ammonium carbonate.\|[0068] Hereinafter, the present invention will be described more fully with reference to the accompanying drawings, in which exemplary embodiments of the invention are shown. This invention may, however, be embodied in many different forms and should not be construed as limited to the exemplary embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art. In the drawings, lengths and sizes of layers and regions may be exaggerated for clarity.\|[0069] As used herein, the term “and/or” includes any and all combinations of one or more of the associated listed items. The invention illustratively described herein may suitably be practiced in the absence of any element or elements, limitation or limitations, not specifically disclosed herein. Thus, for example, the terms “comprising”, “including”, “containing”, etc. shall be read expansively and without limitation. Additionally, the terms and expressions employed herein have been used as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the invention claimed. Thus, it should be understood that although the present invention has been specifically disclosed by preferred embodiments and optional features, modification and variation of the inventions embodied therein herein disclosed may be resorted to by those skilled in the art, and that such modifications and variations are considered to be within the scope of this invention.\|[0070] The invention has been described broadly and generically herein. Each of the narrower species and subgeneric groupings falling within the generic disclosure also form part of the invention. This includes the generic description of the invention with a proviso or negative limitation removing any subject matter from the genus, regardless of whether or not the excised material is specifically recited herein.\|[0071] Other embodiments are within the following claims and non-limiting examples. In addition, where features or aspects of the invention are described in terms of Markush groups, those skilled in the art will recognize that the invention is also thereby described in terms of any individual member or subgroup of members of the Markush group.\|EXPERIMENTAL SECTION\|[0072] Various embodiments described herein relate to a process to convert gaseous carbon dioxide from flue gas into a mineralized form, bound to alkaline earth metals obtained from ultramafic rocks. A general overall equation, employing serpentine (Mg3Si2O5(OH)4) as a representative starting material, to describe the process is as follows:\|Mg3Si2O5(OH)4+3CO2→3MgCO3+2SiO2+2H2O\|[0073] The carbon dioxide is converted into a carbonate, which is thermodynamically more stable and inert. The solid form of the carbonate is easily handled and once bound, the carbon dioxide is not susceptible to re-emission into the atmosphere unless subjected to extreme conditions.\|[0074] Improvements over state-of-the-art mineralization routes include:\|[0075] a) lower energy consumption—It is readily apparent that the net CO2 capture amount for the process described herein is positive, at least in cases where natural gas and oil are the preferred fossil fuels for combustion. This cannot be said for state of the art mineralization processes. The utilization of direct thermal energy significantly contributes to much lower CO2 emissions per ton CO2 captured. In the case of Singapore, which utilizes natural gas as the preferred fuel of choice for power generation, every 2,500 kWh produces one ton of CO2. The amount of CO2 avoided in this case is around 30%, if other assorted electrical energy uses (such as for agitation, milling, and pumping) are taken into account.\|[0076] b) established fundamentals of reactions—kinetics and thermodynamics of decomposition, as well as processes of producing anhydrous MgCl2 have been studied as MgCl2 is an important precursor to electrolytic production of magnesium metal, and thus is of strategic importance.\|[0077] c) avoidance of messy and uncontrollable side reactions—one distinct advantage of using an HCl as a leaching medium is that the regeneration reaction to yield acid is relatively uncomplicated. There are no unwanted secondary decompositions when heating is applied, unlike when nitrates are involved (there is a possibility of nitrite and nitrous products forming when pyrolysis of the nitrate salt occurs).\|[0078] d) relatively small reactor sizes—the scale of operations, when it comes to carbon capture, often involves millions of tons of material being conveyed and pumped annually. Thus, it is desirable to use concentrated solutions or gases in order to reduce infrastructure and operating costs. In fact, one may even argue that a more concentrated solution facilitates certain steps in the process, such as the evaporation stages. Since magnesium chloride is highly soluble in water, a very concentrated leachate solution may be obtained, and thus only relatively small reactors are required.\|[0079] e) ample opportunities to exploit waste heat streams from industry—heat may conveniently be recycled from many industries. The temperature requirements of this process fall in the medium range, at about 230° C. to 650° C. This may easily be obtained, for example, from the turbine exhaust of a gas fired power plant.\|[0080] f) lower capital costs involved at startup—The equipment used may involve commercially available reactors such as agitated tanks, filters, and columns, thereby reducing the need to invest in new technology to design new reactor types or invest in non-standard equipment before commercialization.\|[0081] g) significantly reduced energy penalty to power plant—As the main form of energy input is heat, there is no need to draw electrical energy from the power plant to drive the process. Thus, apart from some miscellaneous uses such as agitators, pumps etc, there is virtually no energy penalty to the power plant. This goes a long way towards keeping electricity costs to the consumer within acceptable ranges.\|[0082] h) applications towards diverse industries: heavy industries such as steel making, coal gasification, metal refineries and cement making emit a significant amount of CO2 in the manufacturing process. Incidentally, most of these industries involve large amounts of heating, and thus produce a lot of waste heat as well. Processes disclosed herein consume waste heat and sequesters CO2, and would be a particularly suitable candidate to partner these industries.\|[0083] Various embodiments seek to eliminate formation of ammonium chloride in the first place, thus avoiding additional regeneration steps and their associated complications altogether. As a substitute, metal chloride hydrolysis is employed as the preferred method to regenerate HCl.\|[0084] There may be four distinct stages to the process, namely: 1) acid digestion of ultramafic mineral raw material; 2) removal of impurities from the leachate solution and concurrent evaporation of water; 3) regeneration of acid for further reuse in the acid digestion step; and 4) the actual mineralization reaction to produce alkaline earth metal carbonates from carbon dioxide.\|[0085] The description of the process, from this point on, will use serpentine, which is a form of ultramafic rock material, as a representative starting mineral for illustration purposes.	(US9896741)\|TECHNICAL FIELD\|[0002] The invention relates to methods of producing metal carbonate from an ultramafic rock material.\|BACKGROUND\|[0003] Heavy industries such as steel making, coal gasification, metal refineries, power plants and cement making units emit a significant amount of carbon dioxide (CO2). Taking Singapore, for example, it was estimated that amount of carbon dioxide from power plants will exceed 20 million tonnes per year for the next decade (see TABLE 1).\|[0004] TABLE 1 Carbon dioxide (CO2) emissions from power plants in Singapore (2007-2017) 2007 Energy and CO2 Emission2017 Energy and CO2 Emission CO2Emission CO2Emission EnergyEmissionrateEnergyEmissionratePower PlantMWh/aMt CO2/at CO2/hrMWh/aMt CO2/at CO2/hr TUAS8,867,2754.0045717,100,00013.201507PULAU SERAYA8,297,8683.9344813,000,0006.00685SENOKO11,200,0004.4550811,500,0004.56520PULAU MERLIMAU0 2,931,1241.29147ISLAND POWER0 2,537,8751.27145PULAU SAKRA2,090,1030.871002,177,4970.91104SINGAPORE CHEMICAL684,5770.38431,610,5930.8395JURONG325,7140.1518363,8600.1719SINGAPORE OLEFINS318,4060.1517332,2270.1618CHANGI WWTP257,3030.1214276,9990.1315SMPO COGEN173,3210.1112182,3920.1113PASIR PANJANG185,0810.0910200,6640.1011Total32,399,64814.3 52,213,23028.7 Source: http://carma.org/region/detail/169\|[0005] Carbon dioxide capture and storage by mineralization has been proposed as a possible technology to reduce global carbon dioxide levels. The technology may include extracting cations from feed material such as rocks, and combining the cations with carbon dioxide to form a stable carbonate material. Due to the large quantities (gigatonnes) of material involved, ability to extract metal from the feed material at high efficiencies is important. Limitations to existing processes include low metal extraction yields and high energy consumption, due to removal of water which has high latent and sensible heat.\|[0006] In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|SUMMARY\|[0007] In a first aspect, a method of producing a metal carbonate from an ultramafic rock material is provided. The method comprises\| - a) providing an ultramafic rock material comprising a metal silicate;\| - b) reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| - c) contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| - d) heating the resultant mixture from step c) to decompose the salt of the metal to form metal oxide; and\| - e) reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|[0013] In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided. The system comprises\| - a) a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| - b) an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| - c) a furnace configured to heat the resultant mixture from step b) to decompose the salt of the metal to form the metal oxide; and\| - d) a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to form the metal carbonate.\|(US9896741)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] The invention will be better understood with reference to the detailed description when considered in conjunction with the non-limiting examples and the accompanying drawings, in which:\|[0019] FIG. 1 is a schematic diagram depicting working mechanism of an air stripper column. Notations in the figures represent the following: 101: packed column; 102: packing material; 103: packing support; 104: packing restrainer; 105: liquid redistributors; 106: blower assembly; 111: contaminant influent; 112: spray; 113: air in; 114: gas out to atmosphere or secondary treatment; and 115: treated effluent.\|[0020] FIG. 2 is a schematic diagram showing process flow for a mineralization process according to an embodiment.\|[0021] FIG. 3 is a graph showing thermogravimetric analysis (TGA) results of MgCl2.6H2O. Y-axis: weight; x-axis: temperature (° C.).\|[0022] FIG. 4 is a graph showing TGA analysis of magnesium carbonate product from reaction of MgO with (NH4)2CO3. Y-axis: weight (mg); x-axis: temperature (° C.).\|[0023] FIG. 5 is a schematic diagram showing general process flow for a system to carry out mineralization process according to embodiments.\|(US9896741)\|DETAILED DESCRIPTION\|[0024] Using methods disclosed herein, carbon dioxide emitted from various sources, such as coal gasification and power plants, may be captured in the form of metal carbonates such as magnesium carbonate, without significant modification of existing infrastructure. The metal carbonates are thermodynamically stable and inert, and once bound, the carbon dioxide that is captured is not susceptible to re-emission into the atmosphere. Furthermore, the metal carbonates produced may be in solid form to render their ease of handling.\|[0025] Various embodiments disclosed herein are particularly suited for long-term sequestration of carbon dioxide emitted from industries. Advantageously, systems for producing metal carbonate disclosed herein may be integrated into existing infrastructure of industries so as to utilize waste heat from the industries in production of metal carbonates. The metal carbonates produced may be used as building materials or for land reclamation purposes, or be used as additives for adding to polymers as fire retardants.\|[0026] With the above in mind, various embodiments refer in a first aspect to a method of producing a metal carbonate from an ultramafic rock material.\|[0027] The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|[0028] As used herein, the term “ultramafic rock material” refers to igneous and meta-igneous rocks which are composed of more than 90% mafic minerals in various proportions with trace amounts of other minerals. The term “mafic” is used to describe a silicate mineral or rock that is rich in magnesium. Apart from magnesium, the ultramafic rock material may also contain metals such as iron, nickel, chromium, manganese and/or calcium as impurities.\|[0029] Main mafic minerals include olivine (Mg2SiO4), orthopyroxene (MgSiO3), and clinopyroxene ((MgCa)SiO3). Upon hydration, the corresponding mafic minerals are serpentine (Mg3Si2O5(OH)4), tremolite (Mg5Ca2Si8O22(OH)2), and talc (Mg3Si4O10(OH)2).\|[0030] Of particular importance is serpentine, as it is volumetrically dominant on a global scale. Typically, serpentine has a silica content of less than 45%, magnesium oxide content of greater than 18%, and a high iron oxide content in the range of about 5% to 15%. Content of serpentine may vary between the stated ranges depending on source and quality of the rock. TABLE 2 depicts composition of serpentine according to an embodiment. The values are obtained from direct measurements of the mineral samples using X-ray fluorescence spectroscopy.\|[0031] TABLE 2 Composition of Serpentine (Percentage expressed in terms of weight% of the respective oxides contained within the material)ElementMgOSiO2Fe2O3Al2O3Cr2O3CaONiOMnO Percent46.7242.78.40.610.450.40.290.14 \|[0032] In various embodiments, the ultramafic rock material comprises or consists of serpentine.\|[0033] As mentioned above, the ultramafic rock material is rich in magnesium. Accordingly, in various embodiments, the method of producing metal carbonate from an ultramafic rock material is used to produce magnesium carbonate. Molar ratio of metal to carbonate (CO3) in the metal carbonate may be in the range of about 1:1 to about 5:4. In various embodiments, molar ratio of metal to CO3 in the metal carbonate is about 1:1.\|[0034] The method includes providing an ultramafic rock material comprising a metal silicate. In various embodiments, the metal silicate is magnesium silicate, such as Mg3Si2O5(OH)4. Apart from magnesium silicate, silicates of other metals contained in the ultramafic rock material may also be present, such as silicates of iron, nickel, chromium, manganese, and/or calcium.\|[0035] Providing an ultramafic rock material comprising a metal silicate may include physically working the ultramafic rock material such as by crushing or grinding, so as to reduce size of the ultramafic rock material. Advantageously, by reducing size of the ultramafic rock material, liberation of metal from the ultramafic rock material may be accelerated.\|[0036] In some embodiments, providing an ultramafic rock material includes physically working the ultramafic rock material to form ultramafic rock particles having a size of 0.5 mm or less. Size of the ultramafic rock particles may be characterized by its maximal dimension, wherein the term “maximal dimension” refers to the maximal length of a straight line segment passing through the center of a figure and terminating at the periphery.\|[0037] For example, the ultramafic rock material may comprise or consist of ultramafic rock particles having a size of 0.5 mm or less, such as a size in the range of about 0.01 mm to about 0.5 mm, about 0.05 mm to about 0.5 mm, about 0.1 mm to about 0.5 mm, about 0.2 mm to about 0.5 mm, about 0.01 mm to about 0.3 mm, about 0.01 mm to about 0.1 mm, or about 0.1 mm to about 0.3 mm.\|[0038] The method includes reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal. In reacting the ultramafic rock material with an acid, metal from the ultramafic rock material may be leached out in the form of a metal salt. Hence, the mixture containing the salt of the metal may otherwise be termed as the leachate. A solid residue of coarse silica may also be obtained following reacting of the ultramafic rock material with acid.\|[0039] The acid may, for example, be selected from the group consisting of hydrohalic acid, sulfuric acid (H2SO4), nitric acid (HNO3), phosphoric acid (H3PO4), acetic acid (CH3COOH), and combinations thereof. Depending on the acid used, different metal salts may be formed. For example, salt of the metal may be a halide such as a chloride or a bromide, a sulfate, a nitrate, a phosphate, and/or an acetate. In various embodiments, the acid is a hydrohalic acid, such as hydrofluoric acid (HF), hydrochloric acid (HCl), hydrobromic acid (HBr), and/or hydroiodic acid (HI). In some embodiments, the acid comprises or consists of hydrochloric acid and/or hydrobromic acid.\|[0040] In specific embodiments, the acid comprises or consists of hydrochloric acid. By reacting the ultramafic rock material with hydrochloric acid, metal may be leached from the ultramafic rock material as metal chloride. Use of hydrochloric acid has been found by the inventors to be advantageous, as hydrochloric acid is able to leach metal effectively from ultramafic rock material, and may be regenerated easily and simply without complication. Undesirable decompositions do not take place upon heating of metal chlorides, as opposed to the case of metal nitrates formed from reacting metal silicates with nitric acid, for example, which may generate nitrite and nitrous products.\|[0041] The mixture may accordingly contain chlorides of magnesium, iron, nickel, chromium, manganese, and/or calcium. Due to the high magnesium content in ultramafic rock material, the salt of the metal may mainly be made up of magnesium chloride.\|[0042] In various embodiments, concentration of the hydrochloric acid is at least 27 wt % HCl. For example, concentration of the hydrochloric acid may be at least 30 wt %, at least 35 wt % HCl, or be in the range of about 27 wt % to about 35 wt %, about 27 wt % to about 32 wt %, or about 27 wt % to about 30 wt % HCl.\|[0043] Reacting the ultramafic rock material with an acid may be carried out at a temperature in the range of about 80° C. to about 100° C. For example, reacting the ultramafic rock material with an acid may be carried out at a temperature in the range of about 80° C. to about 95° C., about 80° C. to about 90° C., about 80° C. to about 85° C., about 90° C. to about 100° C., or about 85° C. to about 95° C. In various embodiments, reacting the ultramafic rock material with an acid is carried out under continuous stirring to accelerate liberation of metal from the ultramafic rock material.\|[0044] The method includes contacting the mixture comprising a salt from the metal with oxygen. The oxygen may be in the form of an oxygen flow and/or an air flow. This may be carried out to aerate impurities in the mixture and/or to remove residual acid from the mixture. As mentioned above, the ultramafic rock material may also contain metals such as iron, nickel, chromium, manganese and/or calcium as impurities. By contacting the mixture comprising a salt of the metal with oxygen, the metals may be aerated to their respective oxides and may be precipitated out from the mixture to allow their removal from the resultant mixture by a separation process such as decanting or filtering.\|[0045] By way of example only, this aeration process may be illustrated using hydrochloric acid and iron. Iron may be leached from ultramafic rock material using hydrochloric acid to form iron (II) chloride (FeCl2). The iron (II) chloride may be oxidized readily to iron (III) chloride (FeCl3) upon contact with oxygen, as shown in equation (1):\|12FeCl2+3O2→2Fe2O3+8FeCl3 (1)\|[0046] The iron (III) chloride may undergo auto-hydrolysis in solution to form iron (III) oxide and hydrogen chloride, as shown in equation (2):\|2FeCl3+3H2O→Fe2O3+6HCl (2)\|[0047] Iron (III) oxide may be precipitated out from the mixture following oxidation to allow their easy removal.\|[0048] In various embodiments, contacting the mixture comprising a salt of the metal with oxygen to aerate impurities in the mixture comprises separating oxides of iron, nickel, chromium, aluminum and/or manganese from the resultant mixture following oxidation.\|[0049] Further, from equation (2), it may be seen that by eliminating hydrochloric acid from the solution, conversion of iron (III) chloride into iron (III) oxide may be promoted. This means that metal impurities in the mixture may be removed to a greater extent by removing hydrochloric acid from the mixture. Advantageously, the removal of hydrochloric acid, which may arise from the auto-hydrolysis process as well as residual acid present in the mixture, may be carried out by contacting the mixture comprising a salt of the metal with oxygen.\|[0050] Contacting the mixture comprising a salt of the metal with oxygen may be carried out in a flow of air and/or oxygen. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out by air stripping. As used herein, the term “air stripping” refers to a process by which an air stream is used to remove dissolved gases or volatile components of a liquid. The air stripping may be carried out in an air stripper column. For example, the mixture comprising a salt of the metal may be introduced at the top of an air stripper column. The air stripper column may contain packing material to provide a larger contact surface area for aeration. Air may be introduced at the bottom of the air stripper column, such that the mixture flows in opposite direction to the ascending air while contacting each other. In so doing, the air may strip acid from the mixture. The air exits from the top of the air stripper column, while the resultant mixture, which has been at least partially stripped of acid, may leave the bottom of the air stripper column for channeling into a subsequent stage.\|[0051] In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out under conditions such that pH of the mixture is less than or equal to 9. For example, the contacting may be carried out under conditions such that pH of the mixture is in the range of about 3 to about 9, about 5 to about 9, about 7 to about 9, about 3 to about 7, about 3 to about 5, about 5 to about 7, or about 4 to about 6.\|[0052] Contacting the mixture comprising a salt of the metal with oxygen may be carried out at a temperature in the range of about 150° C. to about 250° C., such as about 180° C. to about 250° C., about 200° C. to about 250° C., about 150° C. to about 220° C., about 150° C. to about 200° C., about 180° C. to about 220° C., or about 180° C. to about 200° C. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature in the range of about 180° C. to about 200° C. In some embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature of about 200° C.\|[0053] By contacting the mixture comprising a salt of the metal with oxygen at elevated temperatures, water may be evaporated or vaporized from the mixture to form steam. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out for a time period suitable to form a mixture saturated with the salt. Advantageously, by removing water from the mixture, this minimizes water content in the mixture for removal in a subsequent stage. At the same time, heat energy may be recovered in the form of steam for rechanneling back into the process.\|[0054] By removing water from the mixture, a hydrated salt of the metal may also be formed. In various embodiments, the hydrated salt of the metal comprises or consists essentially of magnesium chloride hydrates. Water of crystallization of the hydrated metal salt may be in the range of about 2 to about 6, such as 2, 3, 4, 5, or 6.\|[0055] The method of the first aspect includes heating the resultant mixture following contact with oxygen to decompose the salt of the metal to form metal oxide. For example, the metal oxide may contain magnesium oxide, along with trace amounts of oxides of iron, nickel, chromium, manganese, and/or calcium which may not have been removed in an earlier stage.\|[0056] In various embodiments, heating the resultant mixture is carried out at a temperature in the range of about 400° C. to about 600° C., such as about 450° C. to about 600° C., about 500° C. to about 600° C., about 550° C. to about 600° C., about 400° C. to about 550° C., or about 450° C. to about 550° C. In specific embodiments, heating the resultant mixture is carried out at a temperature of about 550° C.\|[0057] Given the high temperatures, steam may be generated. In embodiments where the acid is hydrochloric acid, and where residual acid is present in the resultant mixture not removed in an earlier stage, hydrogen chloride gas may additionally be produced.\|[0058] The metal oxide is reacted with aqueous ammonium carbonate to obtain the metal carbonate. At the same time, aqueous ammonia may be produced.\|[0059] The aqueous ammonium carbonate may be obtained by reacting carbon dioxide with aqueous ammonia, which may be carried out in a gas-liquid packed column. The carbon dioxide may be comprised in a flue gas, which may be channeled from heavy industries such as a power plant.\|[0060] Molar ratio of aqueous ammonia to carbon dioxide may be in the range of about 2:1 to about 2.5:1, such as about 2.1:1, 2.2:1, 2.3:1, 2,4:1, or about 2.5:1.\|[0061] In various embodiments, reacting carbon dioxide with aqueous ammonia is carried out at a pH of at least 9 to maximize degree of carbonation. For example, reacting carbon dioxide with aqueous ammonia may be carried out at a pH in the range of about 9 to about 13, about 9 to about 12, about 9 to about 11, about 9 to about 10, about 10 to about 13, about 11 to about 13, or about 10 to about 12. In some embodiments, reacting carbon dioxide with aqueous ammonia is carried out at a pH of at least 10.\|[0062] Advantageously, reacting the metal oxide with aqueous ammonium carbonate may be carried out at ambient conditions.\|[0063] In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided. The system comprises a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal; an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen to aerate impurities in the mixture and/or to remove residual acid from the mixture; a furnace configured to heat the resultant mixture to decompose the salt of the metal to form the metal oxide; and a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. Schematic diagram of a system for producing a metal carbonate from ultramafic rock material according to embodiments is shown in FIG. 5 and discussed in Example 8. Processing conditions for operating the various components of the system have already been discussed above.\|[0064] In various embodiments, the system further comprises a gas-liquid packed column arranged upstream of the precipitator and configured to carry out reaction of carbon dioxide with aqueous ammonia to form aqueous ammonium carbonate. As mentioned above, the carbon dioxide may be comprised in a flue gas, which may be channeled from heavy industries such as a power plant. The ammonium carbonate that is formed may be used to react with the metal oxide to form metal carbonate. In so doing, carbon dioxide may be captured in the metal carbonate which is thermodynamically stable and inert, thereby rendering the carbon dioxide that is captured not susceptible for re-emission into the atmosphere.\|[0065] The system may further comprise a compressor configured to compress acid vapor and/or water vapor from the air stripper column. This allows formation of higher quality steam that may be used to supplement heating medium that may be used for operating the air stripper column.\|[0066] The system may, in various embodiments, comprise recycling means configured to recycle acid vapor and/or water vapor from the air stripper column and/or the furnace to the reactor and/or the air stripper column. In so doing, heat energy that is generated from the air stripper column and/or the furnace may be reused in other parts of the process, thereby minimizing energy consumption of the system.\|[0067] In various embodiments, the system further comprises recycling means configured to recycle aqueous ammonia from the precipitator to the gas-liquid packed column. As mentioned above, metal oxide may be reacted with aqueous ammonium carbonate to obtain metal carbonate in the precipitator, while producing aqueous ammonia at the same time. By recycling the aqueous ammonia produced to the gas-liquid packed column, the aqueous ammonia may be reused to react with carbon dioxide to form aqueous ammonium carbonate.\|[0068] Hereinafter, the present invention will be described more fully with reference to the accompanying drawings, in which exemplary embodiments of the invention are shown. This invention may, however, be embodied in many different forms and should not be construed as limited to the exemplary embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art. In the drawings, lengths and sizes of layers and regions may be exaggerated for clarity.\|[0069] As used herein, the term “and/or” includes any and all combinations of one or more of the associated listed items. The invention illustratively described herein may suitably be practiced in the absence of any element or elements, limitation or limitations, not specifically disclosed herein. Thus, for example, the terms “comprising”, “including”, “containing”, etc. shall be read expansively and without limitation. Additionally, the terms and expressions employed herein have been used as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the invention claimed. Thus, it should be understood that although the present invention has been specifically disclosed by preferred embodiments and optional features, modification and variation of the inventions embodied therein herein disclosed may be resorted to by those skilled in the art, and that such modifications and variations are considered to be within the scope of this invention.\|[0070] The invention has been described broadly and generically herein. Each of the narrower species and subgeneric groupings falling within the generic disclosure also form part of the invention. This includes the generic description of the invention with a proviso or negative limitation removing any subject matter from the genus, regardless of whether or not the excised material is specifically recited herein.\|[0071] Other embodiments are within the following claims and non-limiting examples. In addition, where features or aspects of the invention are described in terms of Markush groups, those skilled in the art will recognize that the invention is also thereby described in terms of any individual member or subgroup of members of the Markush group.\|EXPERIMENTAL SECTION\|[0072] Various embodiments described herein relate to a process to convert gaseous carbon dioxide from flue gas into a mineralized form, bound to alkaline earth metals obtained from ultramafic rocks. A general overall equation, employing serpentine (Mg3Si2O5(OH)4) as a representative starting material, to describe the process is as follows:\|Mg3Si2O5(OH)4+3CO2→3MgCO3+2SiO2+2H2O\|[0073] The carbon dioxide is converted into a carbonate, which is thermodynamically more stable and inert. The solid form of the carbonate is easily handled and once bound, the carbon dioxide is not susceptible to re-emission into the atmosphere unless subjected to extreme conditions.\|[0074] Improvements over state-of-the-art mineralization routes include:\|[0075] a) lower energy consumption—It is readily apparent that the net CO2 capture amount for the process described herein is positive, at least in cases where natural gas and oil are the preferred fossil fuels for combustion. This cannot be said for state of the art mineralization processes. The utilization of direct thermal energy significantly contributes to much lower CO2 emissions per ton CO2 captured. In the case of Singapore, which utilizes natural gas as the preferred fuel of choice for power generation, every 2,500 kWh produces one ton of CO2. The amount of CO2 avoided in this case is around 30%, if other assorted electrical energy uses (such as for agitation, milling, and pumping) are taken into account.\|[0076] b) established fundamentals of reactions—kinetics and thermodynamics of decomposition, as well as processes of producing anhydrous MgCl2 have been studied as MgCl2 is an important precursor to electrolytic production of magnesium metal, and thus is of strategic importance.\|[0077] c) avoidance of messy and uncontrollable side reactions—one distinct advantage of using an HCl as a leaching medium is that the regeneration reaction to yield acid is relatively uncomplicated. There are no unwanted secondary decompositions when heating is applied, unlike when nitrates are involved (there is a possibility of nitrite and nitrous products forming when pyrolysis of the nitrate salt occurs).\|[0078] d) relatively small reactor sizes—the scale of operations, when it comes to carbon capture, often involves millions of tons of material being conveyed and pumped annually. Thus, it is desirable to use concentrated solutions or gases in order to reduce infrastructure and operating costs. In fact, one may even argue that a more concentrated solution facilitates certain steps in the process, such as the evaporation stages. Since magnesium chloride is highly soluble in water, a very concentrated leachate solution may be obtained, and thus only relatively small reactors are required.\|[0079] e) ample opportunities to exploit waste heat streams from industry—heat may conveniently be recycled from many industries. The temperature requirements of this process fall in the medium range, at about 230° C. to 650° C. This may easily be obtained, for example, from the turbine exhaust of a gas fired power plant.\|[0080] f) lower capital costs involved at startup—The equipment used may involve commercially available reactors such as agitated tanks, filters, and columns, thereby reducing the need to invest in new technology to design new reactor types or invest in non-standard equipment before commercialization.\|[0081] g) significantly reduced energy penalty to power plant—As the main form of energy input is heat, there is no need to draw electrical energy from the power plant to drive the process. Thus, apart from some miscellaneous uses such as agitators, pumps etc, there is virtually no energy penalty to the power plant. This goes a long way towards keeping electricity costs to the consumer within acceptable ranges.\|[0082] h) applications towards diverse industries: heavy industries such as steel making, coal gasification, metal refineries and cement making emit a significant amount of CO2 in the manufacturing process. Incidentally, most of these industries involve large amounts of heating, and thus produce a lot of waste heat as well. Processes disclosed herein consume waste heat and sequesters CO2, and would be a particularly suitable candidate to partner these industries.\|[0083] Various embodiments seek to eliminate formation of ammonium chloride in the first place, thus avoiding additional regeneration steps and their associated complications altogether. As a substitute, metal chloride hydrolysis is employed as the preferred method to regenerate HCl.\|[0084] There may be four distinct stages to the process, namely: 1) acid digestion of ultramafic mineral raw material; 2) removal of impurities from the leachate solution and concurrent evaporation of water; 3) regeneration of acid for further reuse in the acid digestion step; and 4) the actual mineralization reaction to produce alkaline earth metal carbonates from carbon dioxide.\|[0085] The description of the process, from this point on, will use serpentine, which is a form of ultramafic rock material, as a representative starting mineral for illustration purposes.\|(US9896741)\|Example 1: Acid Digestion of Ultramafic Mineral Raw Material and Purification of Leachate\|[0086] Serpentine, ground to particles with sizes of 0.5 mm or less, was reacted with an acid, preferably hydrochloric acid (HCl) to leach out the magnesium contained therein:\|Mg3Si2O5(OH)4(s)+6HCl(aq)→3 MgCl2(aq)+2SiO2(s)+5H2O (1)\|[0087] This extraction step is conducted at 80° C. to 100° C. in a continuously stirred tank reactor (CSTR).\|[0088] The selection of acid used is of great importance, as it affects the reactor sizes and regeneration steps, as can be seen from descriptions later in the text. At least five types of commonly available acids (HCl, H2SO4, HNO3, H3PO4 and CH3COOH) were considered for the leaching step. Of the acids considered, HCl fulfils both the requirements of effective leaching and complication-free regeneration.\|[0089] Magnesium salts of SO42− and PO43− were poorly soluble, necessitating larger reactors to accommodate the more dilute solution produced. Magnesium acetate was reasonably soluble, but the leaching rate was unsatisfactory due to acetic acid being a weak acid. Only Mg(NO3)2 offered comparable solution concentrations and leaching rates to MgCl2. The kinetics of decomposition of Mg(NO3)2, however, is considerably more complicated and less well defined, as it involves the uncontrolled formation of numerous nitrogen species.\|Example 2: Removal of Impurities from Leachate Solution and Concurrent Evaporation of Excess Water\|[0090] Iron, nickel, chrome, manganese and calcium also exist in serpentine ore as impurities such as that shown in TABLE 2. Since it is nearly impossible to inhibit the co-extraction of these elements during the acid leaching step, it is necessary to remove them in a separate step to separate Fe, Ni, Mn and Cr oxides, which are high value added metal salts, to ensure that high purity magnesite is obtained at the end of the process. To this extent, the leachate solution is first filtered to remove the remaining silica. Next, iron dissolved in the leachate solution is precipitated either as hematite or any of its hydrated forms.\|[0091] To accomplish this, the iron-containing leachate is passed through a heated air stripper to aerate the leachate solution and to flush off any remaining unreacted HCl that is dissolved in solution. Dissolved HCl is removed from the solution via contact with supplied air from the bottom of the stripper column, FIG. 1 describes the mechanisms of an air stripper column.\|[0092] The rationale behind this stripping step is based on the facts that 1) ferrous chloride may be readily oxidized to ferric chloride via contact with oxygen:\|12FeCl2+3O2→2Fe2O3+8FeCl3 \|[0093] and 2) iron chlorides in solution may undergo auto-hydrolysis to form iron oxides and hydrogen chloride:\|2FeCl3+3H2O→Fe2O3+6HCl\|[0094] When combined, both reactions may result in the near-total conversion of iron chlorides into iron oxide solids.\|[0095] Degree of auto-hydrolysis is governed by the following equation:\|[0096] \|[0097] Thus, it may be seen that by eliminating HCl from the solution, conversion of FeCl3 into iron oxides may be promoted which may be conveniently filtered from the leachate solution. After removing the iron content, the filtrate is essentially a near saturated MgCl2 solution. It should be noted that the iron oxidation and hydrolysis steps are ideally conducted at 200° C.\|[0098] Apart from stripping HCl from the leachate solution, excess water may also be evaporated to yield magnesium chloride hexahydrate. It is important for concentration of the solution to be as high as possible, as this minimizes the amount of water that needs to be evaporated in a subsequent stage. A saturated leachate solution (circa 5 M of MgCl2, or about 33 wt %) is ideal for operation purposes. In the case of a 33 wt % leachate solution, 5.11 mols of free water would have to be evaporated to yield 1 mol of MgCl2.6H2O. The required heat for this evaporation is:\|5.11H2O(l)→5.11H2O(g) Tmin=100° C., ΔH=208 kJ/mol\|[0099] At 200° C., the hexahydrate salt also undergoes partial dehydration to produce a tetrahydrate salt, shown in the following equation:\|MgCl2.6H2O(s/l)→MgCl2.4H2O(s/l)+2H2O(g) Tmin=100° C., ΔH=116 kJ/mol\|[0100] The total heat required to allow these transformations to occur was thus estimated to be at 323 kJ/mol MgCl2.\|[0101] The steam evolved from evaporation of excess water in this step may be recompressed in a mechanical vapor recompressor, resulting in higher quality steam that may be used to supplement the heating medium that is required for this step.\|[0102] Scaling due to salt precipitation may be avoided, as at temperatures above 117° C., the hydrated salt melts into a molten salt hydrate (MSH). This molten MgCl2 solution may then be transferred to the acid regeneration stage.\|Example 3: Regeneration of Acid Solution\|[0103] The molten salt hydrate may be decomposed into MgO and HCl, according to the following reactions (see Example 5 below for more information):\|MgCl2.4H2O(s/l)→MgCl2.2H2O(s/l)+2H2O(g) Tmin=134° C., ΔH=134 kJ/mol\|MgCl2.2H2O(s/l)→MgOHCl(s)+HCl(g)+H2O(g) Tmin=218° C., ΔH=141 kJ/mol\|MgOHCl(s)→MgO(s)+HCl(g) Tmin=550° C., ΔH=98 kJ/mol\|[0104] The hydrated salt may first be dehydrated, and then undergoes hydrolysis in the presence of water to give hydrogen chloride gas and magnesium oxide. The overall reaction for decomposing MgCl2.4H2O may thus be:\|MgCl2.4H2O(s)→MgO(s)+2HCl(g)+3H2O(g) T=550° C., ΔH=373 kJ/mol\|[0105] An enormous amount of heat may be carried away from the furnace in the form of water vapour and HCl gas. According to the decomposition reaction formula, 3 mols of water vapour are formed for every mol of MgO produced, as well as 2 mols of HCl gas that when dissolved into water, yields 75 kJ/mol of dissolution heat. This heat may be reused in other parts of the process, most notably the impurity removal and evaporation step. It should be noted that the heat required by the evaporator may be less than the heat carried off by the decomposition products from the furnace.\|[0106] As can be seen from the above, it is possible to recycle waste heat from the furnace to be used in the evaporation step, provided that the following three conditions are met: 1) the leachate solution is sufficiently concentrated (not less than 28 wt % MgCl2); 2) the leachate stream enters the evaporator at not less than 100° C. and 3) proper insulation is applied such that heat losses are not significant.\|[0107] The formed MgO solids at the end of the HCl regeneration step may then be transferred to the CO2 mineralization stage, and the HCl may be reused in the acid leaching reaction.\|Example 4: Mineralization of Carbon Dioxide\|[0108] MgO obtained from the end of the previous stage may be contacted with aqueous ammonium carbonate ((NH4)2CO3) from a CO2 scrubbing process to produce solid magnesium carbonate and aqueous ammonia (see Example 7 below for more information). The solid magnesium carbonate may be filtered off, yielding an ammonia solution that may be reused for CO2 removal. The reaction for CO2 removal from flue gas, via ammonia capture, is shown below (see Example 6 below for more information):\|2NH3(aq)+CO2(g)+H2O(l)→(NH4)2CO3(aq)\|[0109] The CO2 removal may be conducted in a packed scrubbing tower, in order to maximize the contacting surface area of the ammonia solution with CO2 gas. The operating conditions and ratio of NH3 to CO2 should be controlled to stay within an optimal range, to avoid formation of by-products such as ammonium bicarbonate (NH4HCO3) and urea ((NH2)2CO). The recommended molar ratio of NH3 to CO2 is about 2:1 to about 2.5:1.\|[0110] Estimations based on HSC software indicate that the reaction between MgO and aqueous (NH4)2CO3 may be favorable at ambient temperatures and pressures, and is exothermic:\|[0111] TABLE 3 Simulation results from HSC for the reaction between MgO and (NH4)2CO3MgO + (NH4)2CO3(ia) = MgCO3(M) + 2NH3(a) + H2O(l)T (° C.)ΔH (kJ)ΔS (J/K)ΔG (kJ)KLog(K) 0.000−21.872135.220−58.8081.765E+01111.24710.000−19.546143.582−60.2011.278E+01111.10720.000−17.009152.387−61.6819.805E+01010.99130.000−14.338161.344−63.2497.929E+01010.89940.000−11.571170.323−64.9086.726E+01010.82850.000−8.732179.246−66.6565.960E+01010.77560.000−5.836188.071−68.4925.493E+01010.74070.000−2.893196.777−70.4175.246E+01010.72080.0000.093205.353−72.4275.173E+01010.71490.0003.118213.798−74.5235.250E+01010.720100.0006.179222.114−76.7035.470E+01010.738 \|[0112] In conclusion, the entire process may be depicted by FIG. 2.\|Example 5: Hydrolysis of Magnesium Chloride Hexahydrate to Magnesium Oxide\|[0113] Hydrolysis of MgCl2.6H2O was studied via thermogravimetric analysis (TGA). Results are shown in FIG. 3.\|[0114] As may be seen from the figure, the hexahydrate salt was dehydrated at temperatures up to 120° C., losing four moles of water per mole of MgCl2.6H2O. The resulting dihydrate salt underwent a first hydrolysis, liberating one mole of water and one mole of HCl to yield MgOHCl. The first hydrolysis was completed at around 220° C.\|[0115] When further heated to 400° C., the hydroxychloride underwent a second hydrolysis, generating another mole of HCl and leaving behind a solid MgO residue.\|Example 6: Reaction of Carbon Dioxide with Aqueous Ammonia\|[0116] An experiment was conducted to demonstrate feasibility of aqueous ammonia as a sorbent for CO2.\|[0117] 0.5 L of 6 M aqueous ammonia solution was prepared by diluting 0.225 L of stock aqueous ammonia (25 wt %) with 0.275 L deionized (DI) water. The solution was immersed in an ice bath and sparged with carbon dioxide gas (3 bar outlet pressure). The pH and temperature in relation to time was recorded in TABLE 4 below.\|[0118] TABLE 4 Time, pH and temperature of aqueous ammonia solutionTime (h)pHTemperature (° C.) 013120.5127111.614211.318310.984410.754510.584 \|[0119] It may be seen that aqueous ammonia may effectively absorb CO2 under the right conditions. Note that the mass transfer and absorption rates may be significantly improved by using a suitably designed scrubber or gas/liquid contactor.\|Example 7: Reaction of Magnesium Oxide with Ammonium Carbonate\|[0120] 14.4 grams (0.15 mols) of ammonium carbonate was dissolved in 150 ml DI water to produce a 1 M ammonium carbonate solution. 4 grams (0.1 mols) of magnesium oxide was added to this solution and stirred for 1 hour at ambient temperature and pressure. Warming of the solution occurred for the first half hour, suggesting that a carbonation reaction was taking place. After thirty minutes, an apparent cooling of the slurry to room temperature was observed.\|[0121] The solids were filtered from the solution and dried in an oven overnight at 80° C. The dried solids were studied using thermogravimetric analysis (TGA) to determine the degree of carbonation. The results are shown in FIG. 4.\|[0122] The results from the figure show that the sample underwent a slow dehydration at temperatures up to 250° C., and loss of CO2 at temperatures above 400° C.\|[0123] Calculations from the data also indicated a H2O:CO2:MgO ratio of 0.87:0.85:1, suggesting a species similar in composition to hydromagnesite (Mg5(CO3)4(OH)2.4H2O).\|Example 8: Exemplary Embodiment of a System\|[0124] FIG. 5 is a schematic diagram showing general process flow for a system to carry out mineralization process according to embodiments.\|[0125] An aqueous leaching process involving HCl and alkaline-earth silicate minerals may take place in R1. The leaching process in R1 may involve reacting aqueous HCl solution with alkaline-earth silicate minerals at not less than 27 wt % HCl and 80° C. to extract the alkaline-earth elements into a leachate solution from the minerals.\|[0126] The leachate solution (Si) from R1 may be subjected to purification by stripping unreacted HCl from the leachate to precipitate impurities from the liquid phase, which may take place in R2.\|[0127] Removal of impurities in R2 may be aided by oxidation of any intermediate species, for example from ferrous to ferric iron, such that they are more easily removed. The oxidation step in R2 may be conducted by introduction of air or oxygen into the leachate solution.\|[0128] Stripping of HCl in R2 may be controlled such that the pH of the leachate solution goes up to, but does not exceed 9. Stripping of HCl in R2 may be conducted in a temperature range of 150° C. to 250° C., more preferably 180° C. to 200° C. The purified leachate solution from R2 may be subjected to evaporation to produce MgCl2 hydrates, where the water of crystallization is between the numbers of 2 to 6.\|[0129] The above-mentioned chemical transformations may be conducted in a single reactor R2, which may be a heated air stripper. The heated air stripper R2 may be maintained at a temperature not less than 180° C., preferably at 200° C. or more. The evaporated water (S4) from R2 may be recycled to the leaching process in R1. The produced MgCl2 hydrates (S2) from R2 may be subjected to thermal hydrolysis in a furnace R3 to yield MgO (S5), HCl and water vapor. The HCl and water vapor from R3 (S3) may be used as a heating medium for the heated air stripper R2. The HCl and water from R2 (S4) may be recycled to the leaching process in R1.\|[0130] A mechanical vapor recompressing mechanism may be used to compress exiting HCl and water vapor S4 from the heated air stripper R2. The recompressed HCl and water vapor (S4-1) may be used to supplement the heating medium.\|[0131] The aqueous (NH4)2CO3 solution (S6) may be obtained by reacting aqueous NH3 solution with CO2 in flue gas from a CO2 point source, such as a power plant.\|[0132] The CO2 capture reaction in R4 may be conducted in a gas-liquid contacting tower with sufficient packing. The carbonation reaction may be reacted at pH not less than 9, and preferably above 10, to maximize the degree of carbonation.\|[0133] The resulting aqueous NH3 solution from R5 (S7) may be recycled to the scrubbing process in R4.\|[0134] Various embodiments described herein is suitable for mitigation of CO2 emissions from all kinds of industrial sectors, such as power plants, cement plants, and steel plants, without significant modification of existing infrastructure. At the same time, the products may be used as building materials or additives to polymers as fire retardants. Particularly, various embodiments disclosed herein are suitable for long-term sequestration of CO2 emitted from local power plants and the carbonation products, carbonates and sand are utilized for land reclamation purposes in Singapore.\|[0135] The predicted amount of CO2 from local power plants for the next decade (see TABLE 1) exceeds approximately 20 million tonnes per year, which may produce about 60 million tonnes or 25 million m3/a of carbonate and sand by this CO2 sequestration process. On an average scale, the landfill area is projected to expand by 1 km2 per year for the next 10 years. Therefore, various embodiments disclosed herein for application to mineral carbonation process is viewed as a promising approach which provides environmental benefits particularly for Singapore.\|[0136] While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it will be understood by those of ordinary skill in the art that various changes in form and details may be made therein without departing from the spirit and scope of the present invention as defined by the following claims.	Family Number\|(69805816)\|69805816\|Abstract\|(WO201599612 A1)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.\|(AU2014370454 B2)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.\|(SG11201605164Y B)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.(From US9896741 B2)\|(US9896741 B2)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.\|Advantages / Prev. Drawbacks\|(WO201599612 A1)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above- mentioned problems.\|(AU2014370454 B2)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the abovementioned problems.\|(AU2014370454 A1)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the abovementioned problems.\|(US9896741 B2)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|(US20160319395 A1)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|	Environmental technology\|Materials, 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SELF=N	WO201088738\|US4798717\|WO201088738\|US4798717\|US4798717\|US3785797	WO201088738 1878278 WHO=Examiner SELF=N CAT=A\|US4798717 42628151 WHO=Examiner SELF=N CAT=A\|WO201088738 1878278 WHO=Applicant SELF=N\|US4798717 42628151 WHO=Applicant SELF=N\|US4798717 42628151 WHO=Examiner SELF=N\|US3785797 42106785 WHO=Examiner SELF=N		US4798717; WO201088738\|US4798717\|US3785797; US4798717; WO201088738\|	(US9896741)\|Applicant references\|-International Preliminary Report on Patentability for International Application No. PCT/SG2014/000613 dated Jun. 28, 2016, pp. 1-5.\|-Written Opinion for International Application No. PCT/SG2014/000613 dated Mar. 16, 2015, pp. 1-4.\|\|\|\|	GRANTED	(US9896741)\|GRANTED\|(WO2015/099612)\|LAPSED\|(AU2014370454)\|GRANTED\|(SG11201605164Y)\|GRANTED	ALIVE	(US9896741)\|ALIVE\|(WO2015/099612)\|DEAD\|(AU2014370454)\|ALIVE\|(SG11201605164Y)\|ALIVE	(US9896741)\|LEGAL DETAILS FOR US9896741\|Actual or expected expiration date=2035-01-20\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2014-12-23\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US15107870\|Application date=2014-12-23\|Standardized application number=2014US-15107870\|Event publication date=2014-12-23\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:BERNS, DANIEL J\|Event publication date=2014-12-23\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2014-12-23\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 40940-P085WOUS\|Event publication date=2014-12-23\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 185095\|Event publication date=2014-12-23\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular 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state=DEAD\|Status=LAPSED\|Event publication date=2014-12-23\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOSG2014/000613\|Application date=2014-12-23\|Standardized application number=2014WO-SG00613\|Event publication date=2015-07-02\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2015/099612\|Publication stage code=A1\|Publication date=2015-07-02\|Standardized publication number=WO201599612\|Event publication date=2017-06-24\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2014370454\|Actual or expected expiration date=2034-12-23\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2014370454\|Application date in the designated or member state=2014-12-23\|Application number in the 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COUNTRY=SG	\|(WO2015/099612)\|SG\|(AU2014370454)\|AU\|(AU2014370454)\|AU\|(SG11201605164Y)\|SG\|(SG11201605164Y)\|SG	(US9896741)\|NAME=Winstead, P.C.\|(WO2015/099612)\|NAME=VIERING, JENTSCHURA & PARTNER LLP P.O. Box 1088 Rochor Road Rochor Post Office Singapore 911833 , COUNTRY=SG\|(AU2014370454)\|NAME=Phillips Ormonde Fitzpatrick PO Box 323 , CITY=Collins Street West , STATE=VIC , POSTCODE=8007 , COUNTRY=AU\|(AU2014370454)\|NAME=Phillips Ormonde Fitzpatrick PO Box 323 , CITY=Collins Street West , STATE=VIC , POSTCODE=8007 , COUNTRY=AU\|(SG11201605164Y)\|NAME=VIERING, JENTSCHURA & PARTNER LLP P.O. BOX 1088<br/>ROCHOR POST OFFICE<br/>Singapore 911833 , COUNTRY=SG , REG=T06LL1666B\|(SG11201605164Y)\|NAME=VIERING, JENTSCHURA & PARTNER LLP P.O. BOX 1088<br/>ROCHOR POST OFFICE<br/>Singapore 911833 , COUNTRY=SG , REG=T06LL1666B	(US9896741)\|SG; SG; SG\|(US20160319395)\|SG; SG; SG\|(WO2015/099612)\|SG; SG; SG\|\|\|(SG11201605164Y)\|SG; SG; SG\|(SG11201605164Y)\|SG; SG; SG	(US9896741)\|NAME=Bu Jie, CITY=Singapore, COUNTRY=SG \|NAME=Yeo Tze Yuen, CITY=Singapore, COUNTRY=SG \|NAME=Sharratt Paul, CITY=Singapore, COUNTRY=SG\|(US20160319395)\|NAME=Bu Jie, CITY=Singapore, COUNTRY=SG \|NAME=Yeo Tze Yuen, CITY=Singapore, COUNTRY=SG \|NAME=Sharratt Paul, CITY=Singapore, COUNTRY=SG\|(WO2015/099612)\|NAME=BU, Jie c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=YEO, Tze Yuen c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=SHARRATT, Paul c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG\|(AU2014370454)\|NAME=Bu, Jie\|NAME=Yeo, Tze Yuen\|NAME=Sharratt, Paul\|(AU2014370454)\|NAME=Bu, Jie\|NAME=Yeo, Tze Yuen\|NAME=Sharratt, Paul\|(SG11201605164Y)\|NAME=BU, Jie c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=SHARRATT, Paul c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=YEO, Tze Yuen c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG\|(SG11201605164Y)\|NAME=BU, Jie c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=SHARRATT, Paul c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=YEO, Tze Yuen c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG	(WO2015/099612)\|5\|(AU2014370454)\|5\|(US9896741)\|5	3	4			(US9896741)\|WO2015/099612\|(AU2014370454)\|WO2015/099612\|(SG11201605164Y)\|WO2015/099612		(US9896741)\|Number of Claims: NCL=20\|Number of Drawings: NDR=5\|Number of Figures: NFG=5\|Independent Claim Number: ICL=1,16\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=28\|Primary examiner: Berns Daniel\|Art Unit.: ART =1736\|\|(US20160319395)\|Number of Claims: NCL=20\|Number of Drawings: NDR=5\|Number of Figures: NFG=5\|Independent Claim Number: ICL=1,16\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: Berns Daniel\|Art Unit.: ART =1736\|\|(WO2015/099612)\|Number of Claims: NCL=20\|Extended kind: EXTK=x\|\|(AU2014370454)\|Number of Claims: NCL=20\|\|(AU2014370454)\|Number of Claims: NCL=20\|\|(SG11201605164Y)\|Number of Claims: NCL=20\|Number of Pages: NPAGES=34\|\|(SG11201605164Y)\|Number of Claims: NCL=17\|	(US9896741)\|Previous publication: US20160319395 A1 2016-11-03 [US20160319395]	(US9896741)\|ENGLISH (ENG)	(AU2014370454)\|Patent\|(US9896741)\|Patent\|(US20160319395)\|Patent\|(SG11201605164Y)\|Patent\|(AU2014370454)\|Patent\|(SG11201605164Y)\|Patent\|(WO201599612)\|Patent	Titre: (US9896741)\|Method of producing metal carbonate from an ultramafic rock material Résumé: (US9896741)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.	30	Abstract	gpt-4o-mini	no	The focus is on producing metal carbonates from ultramafic rock materials using acid and ammonium carbonate, rather than on accelerating weathering processes for CO₂ capture.
33	US63/641,910P\|US63/716,029P\|US19/092,576	WOUS2025/022798\|US19/092,576	US20250339810\|WO2025/230667	116490379	WO2025/230667 A1 2025-11-06 [WO2025230667]\|US20250339810 A1 2025-11-06 [US20250339810]	2024-05-02\|2024-11-04\|2025-03-27	2025-04-02\|2025-03-27	2025-11-06\|2025-11-06		(US20250339810)\|2045-03-27\|(WO2025/230667)\|2027-11-02	(US20250339810)\|Integrated Ocean Alkalinity Enhancement And Seawater Desalination	(US20250339810)\|A desalination unit processes saltwater feedstock (e.g., seawater) to generate freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a high-salt brine stream. An optional pretreatment unit removes contaminants from the saltwater feedstock before desalination. An electrochemical reactor converts the brine stream into a reduced-salt stream having a salt content lower than the saltwater feedstock by converting salt molecules contained in the brine stream into acid molecules contained in an acid product stream and base molecules contained in a base product stream. A mixing device combines the reduced-salt stream with the saltwater feedstock before the resulting mixture solution is delivered to the desalination unit for desalination. The base product stream leaving the electrochemical reactor may be used for ocean alkalinity enhancement (OAE), and the acid product stream may be used to reduce energy costs associated with crushing/grinding alkaline rock in an enhanced ocean weathering (EOW) process.	EBB CARBON	(US20250339810)\|Ebb Carbon, Inc. ([US])\|(WO2025/230667)\|EBB CARBON, INC. ([US])	LORETZ JEREMY\|PELMAN TODD	(US20250339810)\|Loretz Jeremy\|Pelman Todd	(WO2025/230667)\|BEVER, Patrick ([US])	(US20250339810)\|A benefit of this arrangement is that, when ED apparatus 130A is operated such that reduced-salt stream 111A-2 has a salt concentration lower than that of the saltwater feedstock, less saltwater feedstock must be pumped to and processed by the desalination subsystem (not shown in FIG. 2), thereby reducing both operating energy and maintenance costs in at least some cases.\|Moreover, because greenhouse gas concentrations are already at dangerous levels (i.e., the tub is already dangerously full), there is an urgent need for NETs that are capable of significantly reducing atmospheric CO_2 faster than it is being emitted to achieve safe atmospheric concentration levels (i.e., outflow from the tub's drain must be greater than the reduced inflow from the tap to reduce the tub's water to a safe level).\|Therefore, there is a need to supplement emission reductions with the deployment of NETs, which are systems/processes that serve to reduce existing atmospheric greenhouse gas concentrations by, for example, capturing/removing CO_2 from the air and sequestering it for at least 1,000 years.\|A problem with these EOW strategies is that both the crushing/grinding and dispersing processes require a significant amount of energy.\|Accordingly, by utilizing an electrochemical reactor to remove salt from the brine stream generated by the desalination process, and then utilizing the reduced-salt stream generated by the electrochemical reactor to supplement/dilute the saltwater feedstock directed into the desalination unit, the modified desalination system both mitigates the above-mentioned brine disposition problem and addresses other problems associated with conventional desalination systems.\|Note that the pressure required to force freshwater through a membrane is directly proportional to the feedstock solution's salt content (i.e., saltier water having a relatively high salt concentration requires more pressure than less salty water), but this pressure is limited by the strength of the membrane (i.e., the membrane will rupture if the pressure is too high).\|	(US20250339810)\|1. A desalination system for generating a freshwater stream by removing salt from a saltwater feedstock having a first salt concentration level such that the removed salt is concentrated in a brine stream having a second salt concentration level, the second salt concentration level being higher than the first concentration level, the desalination system comprising: an electrochemical reactor configured to generate a reduced-salt stream by electrochemically processing the brine stream such that the salt contained in the brine stream is converted into acid molecules contained in an acid product stream and base molecules contained in a base product stream, and such that the reduced-salt stream exiting the electrochemical reactor has a third salt concentration that is lower than the first salt concentration; a mixing device configured to combine a saltwater feedstock stream including the saltwater feedstock with at least some of the reduced-salt stream to produce a mixture stream having a fourth salt concentration that is between the first and third salt concentrations; and a desalination unit configured to generate the freshwater stream and the brine stream by processing the mixture stream.\|8. A method for generating a freshwater stream by removing salt from a saltwater feedstock having a first salt concentration level such that the removed salt is concentrated in a brine stream having a second salt concentration level, the second salt concentration level being higher than the first concentration level, the method comprising: generating a reduced-salt stream by electrochemically processing the brine stream such that at least some of the salt contained in the brine stream is converted into acid molecules contained in an acid product stream and base molecules contained in a base product stream, and such that the reduced-salt stream has a third salt concentration that is lower than the first salt concentration; generating a mixture stream having a fourth salt concentration that is between the first and third salt concentrations by combining a saltwater feedstock stream including the saltwater feedstock with the reduced-salt stream; and desalinating the mixture stream to generate the freshwater stream and the brine stream.\|16. A hybrid carbon dioxide removal (CDR) system comprising: an ocean alkalinity enhancement (OAE) subsystem including an electrodialysis device configured to electrochemically process salt obtained from an ocean's seawater such that the salt is converted into a base substance and an acid substance, the OAE subsystem further including an alkaline product generator configured to generate an ocean alkalinity product including the base substance fully dissolved in a salt solution; an enhanced ocean weathering (EOW) subsystem configured to generate an alkaline slurry by combining a portion of the acid substance from the electrodialysis device with an alkaline aggregate such that an accelerated ocean weathering reaction between the alkaline aggregate and the acid substance both neutralizes the acid substance and etches/weakens the alkaline aggregate; and a base delivery subsystem configured to supply the ocean alkalinity product and the alkaline slurry to an ocean such that both the fully dissolved base substance and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification.\|	(US20250339810)\|According to another aspect, at least some of the reduced-salt stream generated by the electrochemical process is mixed/combined with the saltwater feedstock (i.e., such that the saltwater feedstock is effectively diluted by the reduced-salt stream before performing the desalination process), thereby reducing freshwater production costs by reducing the amount of salt that must be filtered/removed from the saltwater feedstock during the desalination process (i.e., in comparison to conventional processes in which only saltwater feedstock is desalinated).\|In an embodiment the present invention is directed to a modified desalination process and associated method that utilizes an electrochemical process to both mitigate the above-mentioned brine disposition problem and address other problems associated with conventional desalination systems/methods.\|The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|	(US20250339810)\|OCEAN ALKALINITY(100,4)\|INTEGRATED OCEAN ALKALINITY(100,1)\|ALKALI AGGREGATE(81,27)\|BRINE STREAM(75,40)\|OCEAN ALKALINITY PRODUCT(72,35)\|OCEAN SEAWATER(72,7)\|FRESHWATER STREAM(66,19)\|FEEDSTOCK(61,63)\|ALKALINE SLURRY(61,28)\|ACCELERATED OCEAN(58,9)\|DESALINIZATION(53,24)\|BRINE DISPOSITION(46,7)\|ELECTROCHEMICAL REACTOR(43,68)\|CRUSHING GRIND ALKALINE ROCK(43,1)\|DESALINIZATION SUBSYSTEM(41,21)\|MEMBRANE DESALINIZATION(41,6)\|RAW SEAWATER(39,6)\|ELECTRODIALYSIS(38,61)\|ACIDIC SUBSTANCE(38,21)\|OCEAN ACIDIFICATION(38,14)\|REMOVING SALT(38,5)\|SALT WATER FEEDSTOCK STREAM(38,5)\|BRINE(37,35)\|MIXTURE STREAM(36,19)\|SALT WATER FEEDSTOCK(33,5)\|SEA(31,36)\|SUBSYSTEM(31,30)\|FRESHWATER PRODUCTION(31,1)\|SALT CONCENTRATION(30,47)\|OUTFALL LOCATION(30,8)\|ACIDIC BUFFER TANK(29,20)\|OCEAN SEAWATER PH LEVEL(29,3)\|TUB DRAIN(29,2)\|ION EXCHANGE MEMBRANE(27,16)\|SEAWATER DESALINIZATION SUBSYSTEM(27,6)\|ETCHED WEAKENED ALKALINE AGGREGATE(27,3)\|ACIDIC PRODUCT STREAM(26,14)\|SALT CONCENTRATION LEVEL(26,4)\|CONCENTRATION LEVEL(26,2)\|GENERATED FRESHWATER(26,2)\|SALT INFLOW RATE(26,2)\|SLURRY GENERATOR(25,8)\|SALTY WATER(25,2)\|FEEDSTOCK SOLUTION SALT CONTENT(25,1)\|MODIFIED DESALINIZATION(23,8)\|ALKALINE PRODUCT GENERATOR(23,2)\|TUB WATER(23,1)\|BASE SUBSTANCE(22,26)\|CONSTANT OUTFLOW(22,3)\|GREENHOUSE GAS ATMOSPHERE(21,2)\|ALKALINE AGGREGATE CAPTURE REDUCE(20,3)\|BASE PRODUCT STREAM(19,18)\|DEPLOYMENT(19,2)\|AQUEOUS ACID SOLUTION(18,13)\|FLUID BUFFERING(18,12)\|BASE DELIVERY SUBSYSTEM(18,7)\|HYBRID CARBON DIOXIDE(18,3)\|SALT CONVERSION(18,2)\|REDUCING AGENT INFLOW(18,1)\|SAFE ATMOSPHERIC CONCENTRATION LEVEL(18,1)\|REDUCED SALT STREAM(17,56)\|FRESHWATER(17,22)\|CHLORIDE ION(17,11)\|DESALINIZATION(17,11)\|SOLUTION SALT CONTENT(17,1)\|URGENT NEED(17,1)\|GREENHOUSE GAS(16,6)\|ATMOSPHERIC CARBON DIOXIDE(16,5)\|BRINY GROUNDWATER(16,5)\|STRATEGY(16,2)\|OCEAN ALKALINITY ENHANCEMENT(15,58)\|BASE BUFFER TANK(15,23)\|ION EXCHANGE STACK(15,19)\|CRUSHING GRINDING(15,4)\|OPPOSING ELECTRODE(15,4)\|INTEGRATING SEAWATER DESALINIZATION(15,2)\|OCEAN SEAWATER ALKALINITY(15,2)\|SALT BRINE STREAM(15,2)\|TUB(15,2)\|DESALINIZATION UNIT(14,42)\|ENHANCED OCEAN WEATHERING(14,38)\|ELECTROCHEMICAL(14,14)\|DANGEROUS LEVEL(14,2)\|DISPERSING(14,1)\|CARBON DIOXIDE(13,12)\|PARTY BUYER(13,6)\|IRRIGATION(13,4)\|OUTFLOW(13,4)\|REACTION TANK(12,7)\|BYPRODUCT BRINE STREAM(12,3)\|EMISSION REDUCTION(12,1)\|BIPOLAR ELECTRODIALYSIS(11,31)\|AQUEOUS BASE SOLUTION(11,13)\|MODIFIED DESALINIZATION(11,3)\|SAFE LEVEL(11,2)\|CATASTROPHIC OCEAN ACIDIFICATION(11,1)\|INTEGRATED DESALINIZATION OCEAN ALKALINITY ENHANCEMENT(10,8)\|COASTAL COMMUNITY(10,2)\|UNPROCESSED BRINE BUILDUP(10,1)\|MIXING TANK(9,10)\|SALT SOLUTION(9,8)\|SUPPLYING ELECTRICITY(9,6)\|OCEAN CAPTURE(9,4)\|ECOLOGICAL HAZARD(9,2)\|SEAWATER DESALINIZATION PLANT(9,2)\|STAND ALONE SEAWATER DESALINIZATION(9,2)\|NEGATIVE EMISSIONS TECHNOLOGIE(8,14)\|HUMAN CONSUMPTION(8,8)\|SALT FEEDSTOCK SOLUTION(8,5)\|MIXTURE SOLUTION(8,4)\|OUTFLOW PORT(8,4)\|ACCELERATED WEATHERING(8,3)\|REVERSE OSMOSIS SEAWATER DESALINIZATION(8,1)\|SHELLFISH DECREASED SURVIVAL(8,1)\|REDUCE SALT STREAM(7,18)\|SODIUM ION(7,10)\|ACIDIC BYPRODUCT(7,4)\|PROCESS FLUID(7,4)\|FILTERED SEAWATER BRINE(7,2)\|LCOC RATING(7,2)\|MINIMIZING LCOC(7,2)\|SALT DISSOCIATION(7,2)\|ALKALINE ROCK CRUSHING GRINDING(7,1)\|BRACKISH GROUNDWATER(7,1)\|DIRECTLY PROPORTIONAL(7,1)\|FEEDSTOCK PRETREATMENT(7,1)\|FRESHWATER AQUIFER(7,1)\|OCEAN DEACIDIFICATION(7,1)\|CARBON DIOXIDE REMOVAL(6,14)\|INPUT MANIFOLD(6,6)\|ELECTROLYTE SOLUTION(6,5)\|CONTAINING PLASTIC(6,3)\|DIVALENT ION(6,3)\|FRESHWATER OUTPUT STREAM(6,3)\|INFLOW PORT(6,3)\|SEMIPERMEABLE MEMBRANE(6,3)\|FEEDSTOCK INFLOW RATE(6,2)\|FILTERING CONTAMINANT(6,2)\|SPOT PRICING(6,2)\|BATHTUB ANALOGY(6,1)\|COORDINATE DESALINIZATION(6,1)\|CRUSHING GRINDING ALKALINE AGGREGATE(6,1)\|ECOLOGICAL CONCERN(6,1)\|GOVERNMENT AUTHORIZATION(6,1)\|OCEAN DISPERSION(6,1)\|OUTFALL BRINE INCREASED SALINITY(6,1)\|PHYSIOLOGICAL CHALLENGE(6,1)\|PROTON DISSOCIATION(6,1)\|SEAWATER FEEDSTOCK SALT CONTENT(6,1)\|SEAWATER HARDNESS(6,1)\|SHARED PLANT FACILITY(6,1)\|WATERTIGHT CONTAINMENT HOUSING(6,1)\|WEAKENED ETCHED ALKALINE AGGREGATE(6,1)\|WIDESPREAD ACCEPTANCE(6,1)\|POST PRODUCTION(5,12)\|MAINTENANCE COST(5,11)\|NAOH(5,10)\|ACIDIC SOLUTION(5,9)\|WEAK ACID STREAM(5,8)\|AQUEOUS SOLUTION(5,7)\|ACIDIC STREAM(5,4)\|CELL ACID CHAMBER(5,4)\|CELL SALT CHAMBER(5,4)\|DESALINIZATION SYSTEM METHOD(5,2)\|FINAL ALKALINE SLURRY(5,2)\|LEAVING REACTOR(5,2)\|MOTIVE(5,2)\|SALT AQUEOUS FEEDSTOCK SOLUTION(5,2)\|DECREASED SEAWATER PH(5,1)\|DISSOCIATED HYDROXIDE ION(5,1)\|DISSOLUTION KINETICS(5,1)\|ETCHED WEAKENED AGGREGATE(5,1)\|MANKIND EFFORT(5,1)\|NEARBY OCEAN(5,1)\|OCEAN ALKALINITY PRODUCT GENERATION(5,1)\|PRECRUSHED GROUND ALKALINE AGGREGATE(5,1)\|PREINDUSTRIAL ERA TEMPERATURE(5,1)\|RAW FEEDSTOCK(5,1)\|REDUCING ECOSAFETY RISK(5,1)\|SEAWATER FEEDSTOCK INPUT(5,1)\|TARGETED CONTAMINANT(5,1)\|UNTREATED FEEDSTOCK(5,1)\|SYSTEM CONTROLLER(4,20)\|ANODE(4,5)\|ENERGY COST(4,3)\|OUTPUT MANIFOLD(4,3)\|SALT BUFFER TANK(4,3)\|TREATED UNTREATED SALT(4,3)\|NANOFILTRATION(4,2)\|ALKALINE AGGREGATE DELIVERY INJECTION(4,1)\|ALKALINE AGGREGATE ROCK(4,1)\|ALKALINE ROCK AGGREGATE(4,1)\|AMBIENT SEA(4,1)\|BIPOLAR MEMBRANE(4,1)\|BRINE CONVERSION(4,1)\|BYPRODUCT STREAM(4,1)\|COARSELY GROUND ALKALINE AGGREGATE(4,1)\|DESALINIZED FLUID(4,1)\|EARTH OCEAN(4,1)\|ELECTROCHEMICAL CONVERSION(4,1)\|HARDNESS RELATED MINERAL HRM(4,1)\|INFLOW SUM(4,1)\|INSTALLATION EXPENSE(4,1)\|PERIODIC MAINTENANCE(4,1)\|PIPE INTERCONNECTION(4,1)\|RECLAIMED METAL SALE(4,1)\|SALT BRINE DISPOSITION(4,1)\|SALT HARDNESS(4,1)\|SILICATE ROCK(4,1)\|SPLIT BRINE(4,1)\|TOTE TANK(4,1)\|TUB FILL(4,1)\|WATER STRESSED COMMUNITY RESILIENCE(4,1)\|HCL(3,13)\|WEAK BASE STREAM(3,7)\|ACID BUFFER TANK(3,6)\|ELECTROCHEMICAL OCEAN ALKALINITY ENHANCEMENT(3,6)\|AQUEOUS SALT SOLUTION(3,5)\|ACID PRODUCTION TANK(3,4)\|BASE PRODUCT TANK(3,3)\|CATHODE(3,3)\|FOSSIL FUEL(3,3)\|ION EXCHANGE FILTER(3,3)\|RESERVOIR(3,3)\|ACIDIC PRODUCT NEUTRALIZATION(3,2)\|BRINE SOLUTION(3,2)\|EMISSION RATE(3,2)\|ION CURRENT(3,2)\|MARINE ORGANISM(3,2)\|OUTFLOW RATE(3,2)\|POSITIVE ELECTRODE(3,2)\|SODIUM TRANSFER(3,2)\|SUPPLYING ENERGY(3,2)\|ULTRAFILTRATION(3,2)\|ACID DISPOSAL(3,1)\|ALKALI PARTICLE(3,1)\|ALKALINE OCEAN PRODUCT(3,1)\|ALKALINE PRODUCTION GENERATOR(3,1)\|ALKALINE SUBSTANCE(3,1)\|BIOPHYSICAL LIMIT(3,1)\|BUFFER RESOURCE(3,1)\|CALCIUM CARBONATE SHELL(3,1)\|CELL SALT INLET(3,1)\|CELL SALT OUTLET(3,1)\|CHLORINE ION(3,1)\|CIRCLED ARROW(3,1)\|CONTINUING DEVELOPMENT(3,1)\|DIRECTLY REVERSE OCEAN ACIDIFICATION(3,1)\|DRASTIC REDUCTION(3,1)\|EARTH ATMOSPHERE(3,1)\|ECONOMIC REASON(3,1)\|ELECTROCHEMICAL PROCESSING(3,1)\|FINAL SALINITY(3,1)\|FRESHWATER NATURAL MOVEMENT(3,1)\|ION PERMEABLE MEMBRANE(3,1)\|LCOCS(3,1)\|LEAVING ELECTROCHEMICAL REACTOR(3,1)\|LIQUID FRESHWATER(3,1)\|MAFICS ULTRAMAFICS(3,1)\|MAINTAINING PRETREATMENT COST(3,1)\|MAJOR CHALLENGE(3,1)\|MEMBRANE B1(3,1)\|MINIMIZING SALT CONTENT(3,1)\|MIXING OUTLET(3,1)\|NET BENEFIT(3,1)\|OCEAN ABILITY(3,1)\|ONLY SALT(3,1)\|OUTLET MANIFOLD(3,1)\|PRECRUSHER GRINDER(3,1)\|PREGRINDING CRUSHING(3,1)\|PRODUCTION EFFICIENCY OPTIMIZATION(3,1)\|PROJECT WIDE OPTIMIZATION(3,1)\|REDUCING LCOC(3,1)\|SEAWATER DESALINIZATION(3,1)\|SEAWATER TREATMENT(3,1)\|SHARED SALT(3,1)\|SLOW INFLOW RATE(3,1)\|WATER INFLOW(3,1)\|112E 31 ROCK AGGREGATE(2,1)\|ACID DOSING PUMP(2,1)\|ADDRESSING(2,1)\|ADVANCED WEATHERING OPERATION VALUABLE(2,1)\|AQUEOUS ACID(2,1)\|AQUEOUS ALKALINE SOLUTION(2,1)\|ARTIFICIAL INTELLIGENCE(2,1)\|BICARBONATE(2,1)\|BUFFERING(2,1)\|CAPITAL EXPENSE REDUCTION(2,1)\|CARBON DIOXIDE TON(2,1)\|CELL ACID INLET(2,1)\|CELL ACID OUTLET(2,1)\|\|(WO2025/230667)\|ALKALI AGGREGATE(100,25)\|SEAWATER DESALINIZATION(100,13)\|OCEAN ALKALINITY(100,7)\|INTEGRATED OCEAN ALKALINITY(100,3)\|BRINE STREAM(91,40)\|OCEAN ALKALINITY PRODUCT(87,35)\|NEUTRALI ZES(81,1)\|FRESHWATER STREAM(80,19)\|OCEAN ACIDI FICATION(80,4)\|ALKALINE SLURRY(74,27)\|ACCELERATED OCEAN(71,9)\|FEEDSTOCK(68,63)\|DESALINIZATION(64,24)\|UTILI ZING(62,5)\|WIDESPREAD ACCEPTANCE(57,1)\|BRINE DISPOSITION(56,7)\|CRUSHING GRIND ALKALINE ROCK(53,1)\|ELECTROCHEMICAL REACTOR(52,70)\|MANKIND EFFORT(51,1)\|MEMBRANE DESALINIZATION(49,6)\|ACIDIC SUBSTANCE(48,17)\|RAW SEAWATER(47,6)\|ELECTRODIALYSIS(45,62)\|REMOVING SALT(45,5)\|SALT WATER FEEDSTOCK STREAM(45,5)\|SEA(44,38)\|BRINE(44,35)\|MIXTURE STREAM(44,19)\|OCEAN ACIDIFICATION(41,10)\|SALT WATER FEEDSTOCK(40,5)\|FRESHWATER PRODUCTION(38,1)\|SUBSYSTEM(37,31)\|OUTFALL LOCATION(36,8)\|SALT CONCENTRATION(35,48)\|TUB DRAIN(35,2)\|SEAWATER(34,32)\|ION EXCHANGE MEMBRANE(33,16)\|SEAWATER DESALINIZATION SUBSYSTEM(33,6)\|ETCHED WEAKENED ALKALINE 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TECHNOLOGIE(12,14)\|ATMOSPHERIC CO2(12,9)\|ACID BUFFER TANK(12,8)\|COASTAL COMMUNITY(12,2)\|GOVERNMENT AUTHORI ZATION(12,1)\|UNPROCESSED BRINE BUILDUP(12,1)\|CARBON DIOXIDE REMOVAL(11,15)\|MIXING TANK(11,10)\|SALT SOLUTION(11,8)\|SUPPLYING ELECTRICITY(11,6)\|OCEAN CAPTURE(11,4)\|ECOLOGICAL HAZARD(11,2)\|SEAWATER DESALINIZATION PLANT(11,2)\|STAND ALONE SEAWATER DESALINIZATION(11,2)\|SUF FICIENT(11,2)\|UTILI ZED(11,2)\|UTILI ZES(11,2)\|ELECTROCHEMICAL ASSISTED OCEAN(11,1)\|SPECI FIC MODIFIED DESALINIZATION(11,1)\|HUMAN CONSUMPTION(10,8)\|SALT FEEDSTOCK SOLUTION(10,5)\|MIXTURE SOLUTION(10,4)\|OUTFLOW PORT(10,4)\|ACCELERATED WEATHERING(10,3)\|ALKALINE AGGREGATE NEUTRALI(10,1)\|MODI FICATION(10,1)\|REVERSE OSMOSIS SEAWATER DESALINIZATION(10,1)\|SHELLFISH DECREASED SURVIVAL(10,1)\|PROCESS FLUID(9,4)\|ETCHED WEAKENED AGGREGATE(9,2)\|SALT DISSOCIATION(9,2)\|ALKALINE ROCK CRUSHING GRINDING(9,1)\|BRACKISH GROUNDWATER(9,1)\|CONFIGURING POSTPRODUCTION(9,1)\|DIRECTLY PROPORTIONAL(9,1)\|EF FECTIVENESS(9,1)\|FEEDSTOCK PRETREATMENT(9,1)\|FRESHWATER AQUIFER(9,1)\|NEUTRALI ZED(9,1)\|OCEAN DEACIDIFICATION(9,1)\|SYSTEM FEATURE(9,1)\|SODIUM ION(8,10)\|ELECTROLYTE SOLUTION(8,5)\|FILTERED SEAWATER BRINE(8,2)\|NAOH(7,10)\|CONTAINING PLASTIC(7,3)\|DIVALENT ION(7,3)\|FRESHWATER OUTPUT STREAM(7,3)\|INFLOW PORT(7,3)\|DESALINIZATION SYSTEM METHOD(7,2)\|FEEDSTOCK INFLOW RATE(7,2)\|FILTERING CONTAMINANT(7,2)\|SPOT PRICING(7,2)\|BATHTUB ANALOGY(7,1)\|COORDINATE DESALINIZATION(7,1)\|CRUSHING GRINDING ALKALINE AGGREGATE(7,1)\|ECOLOGICAL CONCERN(7,1)\|MINIMI ZES(7,1)\|MINIMI ZING SALT CONTENT(7,1)\|OCEAN DISPERSION(7,1)\|OUTFALL BRINE INCREASED SALINITY(7,1)\|PHYSIOLOGICAL CHALLENGE(7,1)\|PROTON DISSOCIATION(7,1)\|SEAWATER FEEDSTOCK SALT CONTENT(7,1)\|SEAWATER HARDNESS(7,1)\|SHARED PLANT FACILITY(7,1)\|WATERTIGHT CONTAINMENT HOUSING(7,1)\|WEAKENED ETCHED ALKALINE AGGREGATE(7,1)\|ACIDIC SOLUTION(6,9)\|WEAK ACID STREAM(6,8)\|AQUEOUS SOLUTION(6,7)\|ACIDIC STREAM(6,4)\|CELL ACID CHAMBER(6,4)\|CELL SALT CHAMBER(6,4)\|INPUT MANIFOLD(6,4)\|ACIDIC BYPRODUCT(6,2)\|ECO SAFETY RISK(6,2)\|INPUT MANI FOLD(6,2)\|LEAVING REACTOR(6,2)\|MOTIVE(6,2)\|SALT AQUEOUS FEEDSTOCK SOLUTION(6,2)\|SEMIPERMEABLE MEMBRANE(6,2)\|ADJ USTS(6,1)\|ALKALINE AGGREGATE INJECTION(6,1)\|CUTTING CO2 EMISSION(6,1)\|DECREASED SEAWATER PH(6,1)\|DISSOCIATED HYDROXIDE ION(6,1)\|DISSOLUTION KINETICS(6,1)\|ECOSAFETY RISK(6,1)\|ELECTROCHEMICAL REACTOR HOD(6,1)\|LCOC RATING(6,1)\|MINIMIZING LCOC(6,1)\|NEARBY OCEAN(6,1)\|OCEAN ALKALINITY PRODUCT GENERATION(6,1)\|OPTIMI ZE(6,1)\|PRECRUSHED GROUND ALKALINE AGGREGATE(6,1)\|PREINDUSTRIAL ERA TEMPERATURE(6,1)\|RAW FEEDSTOCK(6,1)\|SEAWATER FEEDSTOCK INPUT(6,1)\|SETTING ENERGY OCEAN DISPERSAL(6,1)\|TARGETED CONTAMINANT(6,1)\|UNTREATED FEEDSTOCK(6,1)\|POST PRODUCTION(5,8)\|ENERGY COST(5,3)\|SALT BUFFER TANK(5,3)\|TREATED UNTREATED SALT(5,3)\|NANOFILTRATION(5,2)\|ABSORBED CO2(5,1)\|ALKALINE AGGREGATE ROCK(5,1)\|BIPOLAR MEMBRANE(5,1)\|BRINE CONVERSION(5,1)\|BYPRODUCT STREAM(5,1)\|CAPTURED CO2(5,1)\|CO2 DISSOLUTION(5,1)\|COARSELY GROUND ALKALINE AGGREGATE(5,1)\|DESALINIZED FLUID(5,1)\|EARTH OCEAN(5,1)\|HARDNESS RELATED MINERAL HRM(5,1)\|INFLOW SUM(5,1)\|INSTALLATION EXPENSE(5,1)\|MEMBRANE FL(5,1)\|NEGATIVE CO2 EMISSION(5,1)\|OCEAN SEAWATER PH LEVEL(5,1)\|PERIODIC MAINTENANCE(5,1)\|PIPE INTERCONNECTION(5,1)\|RECLAIMED METAL SALE(5,1)\|SALT BRINE DISPOSITION(5,1)\|SALT HARDNESS(5,1)\|SILICATE ROCK(5,1)\|SPLIT BRINE(5,1)\|TOTE TANK(5,1)\|TUB FILL(5,1)\|WATER STRESSED COMMUNITY RESILIENCE(5,1)\|WEAK BASE STREAM(4,7)\|AQUEOUS SALT SOLUTION(4,5)\|ACID PRODUCTION TANK(4,4)\|ANODE(4,4)\|ACIDIC PRODUCT NEUTRALIZATION(4,2)\|BRINE SOLUTION(4,2)\|HYBRID CARBON DIOXIDE(4,2)\|ION CURRENT(4,2)\|MARINE ORGANISM(4,2)\|OUTFLOW RATE(4,2)\|OUTPUT MANIFOLD(4,2)\|POSITIVE ELECTRODE(4,2)\|SIGNI(4,2)\|SODIUM TRANSFER(4,2)\|ULTRAFILTRATION(4,2)\|ALKALI PARTICLE(4,1)\|ALKALINE OCEAN PRODUCT(4,1)\|ALKALINE PRODUCTION GENERATOR(4,1)\|BIOPHYSICAL LIMIT(4,1)\|BUFFER RESOURCE(4,1)\|CALCIUM CARBONATE SHELL(4,1)\|CELL SALT INLET(4,1)\|CELL SALT OUTLET(4,1)\|CHLORINE ION(4,1)\|CIRCLED ARROW(4,1)\|DIRECTLY REVERSE OCEAN ACIDIFICATION(4,1)\|DRASTIC REDUCTION(4,1)\|EARTH ATMOSPHERE(4,1)\|ECONOMIC REASON(4,1)\|ELECTROCHEMICAL PROCESSING(4,1)\|F EEDSTOCK STREAM(4,1)\|FINAL SALINITY(4,1)\|FRESHWATER NATURAL MOVEMENT(4,1)\|ION PERMEABLE MEMBRANE(4,1)\|LCOCS(4,1)\|LEAVING ELECTROCHEMICAL REACTOR(4,1)\|LIQUID FRESHWATER(4,1)\|MAINTAINING PRETREATMENT COST(4,1)\|MAJOR CHALLENGE(4,1)\|MIXING OUTLET(4,1)\|NET BENEFIT(4,1)\|OCEAN ABILITY(4,1)\|ONLY SALT(4,1)\|OUTLET MANIFOLD(4,1)\|OUTPUT MANI FOLD(4,1)\|PRECRUSHER GRINDER(4,1)\|PRODUCTION EFFICIENCY OPTIMIZATION(4,1)\|PROJECT WIDE OPTIMIZATION(4,1)\|REDUCING CO2 EMISSION(4,1)\|REDUCING LCOC(4,1)\|SEAWATER DESALINIZATION(4,1)\|SEAWATER TREATMENT(4,1)\|SENSOR SI(4,1)\|SHARED SALT(4,1)\|SLOW INFLOW RATE(4,1)\|THREAT(4,1)\|WATER INFLOW(4,1)\|ZE SENSOR(4,1)\|MAINTENANCE COST(3,11)\|ELECTROCHEMICAL OCEAN ALKALINITY ENHANCEMENT(3,6)\|BASE PRODUCT TANK(3,3)\|CATHODE(3,3)\|FOSSIL FUEL(3,3)\|ION EXCHANGE FILTER(3,3)\|RESERVOIR(3,3)\|ACID DOSING PUMP(3,1)\|ADDRESSING(3,1)\|AQUEOUS ALKALINE SOLUTION(3,1)\|	(US20250339810)\|1. A desalination system for generating a freshwater stream by removing salt from a saltwater feedstock having a first salt concentration level such that the removed salt is concentrated in a brine stream having a second salt concentration level, the second salt concentration level being higher than the first concentration level, the desalination system comprising:\| an electrochemical reactor configured to generate a reduced-salt stream by electrochemically processing the brine stream such that the salt contained in the brine stream is converted into acid molecules contained in an acid product stream and base molecules contained in a base product stream, and such that the reduced-salt stream exiting the electrochemical reactor has a third salt concentration that is lower than the first salt concentration;\| a mixing device configured to combine a saltwater feedstock stream including the saltwater feedstock with at least some of the reduced-salt stream to produce a mixture stream having a fourth salt concentration that is between the first and third salt concentrations; and\| a desalination unit configured to generate the freshwater stream and the brine stream by processing the mixture stream.\|2. The system of claim 1, further comprising a pretreatment unit configured to generate the saltwater feedstock stream by removing contaminants from a portion of the saltwater feedstock received from an external source.\|3. The system of claim 2, wherein the mixing device is configured such that the mixture stream includes all of the reduced-salt stream received from the electrochemical reactor and such that the mixture stream exiting the mixing device is maintained at a constant outflow rate by adjusting an inflow rate of the saltwater feedstock stream entering the mixing device.\|4. The system of claim 1, wherein the desalination unit comprises one of a thermal desalination system and a membrane-based desalination system.\|5. The system of claim 1, wherein the electrochemical reactor comprises:\| an electrodialysis (ED) apparatus including an ion exchange stack comprising a plurality of chambers arranged in series between opposing electrodes and respectively separated by intervening ion exchange membranes; and\| a flow control system configured to direct the brine stream to a first chamber of the plurality of chambers and to direct the reduced-salt stream from said first chamber, to direct an aqueous acid solution to a second chamber of the plurality of chambers and to direct said acid product stream away from said second chamber, and to direct an aqueous base solution to a third chamber of the plurality of chambers and to direct said base product stream away from said third chamber,\| wherein the ED apparatus is configured such that chloride ions disposed in the brine stream pass from the first chamber through a first ion exchange membrane into the second chamber, and such that sodium ions disposed in the brine stream pass from the first chamber through a second ion exchange membrane into the third chamber.\|6. The system of claim 5, wherein the electrochemical reactor further comprises a fluid buffering system including:\| an acid buffer tank configured to contain the aqueous acid solution directed into said second chamber of the ED apparatus and to receive a first portion of the acid product stream directed away from said second chamber of the ED apparatus; and\| a base buffer tank configured to contain the aqueous base solution directed into said third chamber of the ED apparatus and to receive a first portion of the base product stream directed away from said third chamber of the ED apparatus,\| wherein the flow control system is further configured to direct a portion of the generated freshwater into one or more of said acid buffer tank and said base buffer tank.\|7. The system of claim 1,\| wherein the saltwater feedstock comprises raw seawater obtained from an ocean,\| wherein the system further comprises a post-production unit including at least one of:\| an alkalinity product generation unit configured to generate an ocean alkalinity product using at least a portion of the base product stream such that the ocean alkalinity product includes said base molecules fully dissolved in a salt solution and has a pH level that is a predetermined amount higher than a pH level of the ocean's seawater;\| an enhanced ocean weathering subsystem configured to generate an alkaline slurry using at least a portion of the acid product stream by combining the acid product stream portion with an alkaline aggregate such that a reaction between the alkaline aggregate and the acid molecules both neutralizes the acid molecules and etches the alkaline aggregate; and\| a base delivery system configured to supply at least one of the ocean alkalinity product and the alkaline slurry to the ocean at a designated outfall location.\|8. A method for generating a freshwater stream by removing salt from a saltwater feedstock having a first salt concentration level such that the removed salt is concentrated in a brine stream having a second salt concentration level, the second salt concentration level being higher than the first concentration level, the method comprising:\| generating a reduced-salt stream by electrochemically processing the brine stream such that at least some of the salt contained in the brine stream is converted into acid molecules contained in an acid product stream and base molecules contained in a base product stream, and such that the reduced-salt stream has a third salt concentration that is lower than the first salt concentration;\| generating a mixture stream having a fourth salt concentration that is between the first and third salt concentrations by combining a saltwater feedstock stream including the saltwater feedstock with the reduced-salt stream; and\| desalinating the mixture stream to generate the freshwater stream and the brine stream.\|9. The method of claim 8, further comprising generating the saltwater feedstock stream by removing contaminants from a portion of the saltwater feedstock received from an external source.\|10. The method of claim 9, wherein generating the mixture stream comprises utilizing all of the reduced-salt stream received from the electrochemical reactor and maintaining the mixture stream at a constant outflow rate by adjusting an inflow rate of the saltwater feedstock stream.\|11. The method of claim 8, wherein desalinating the mixture stream comprises utilizing one of a thermal desalination system and a membrane-based desalination system.\|12. The method of claim 8, wherein generating a reduced-salt stream comprises:\| directing the brine stream through a first chamber while directing an aqueous acid solution to a second chamber and directing an aqueous base solution to a third chamber, the first chamber being disposed between the second chamber and the third chamber;\| applying an electric field across the first, second and third chambers such that chloride ions disposed in the brine stream pass from the first chamber through a first ion exchange membrane into the second chamber, and such that sodium ions disposed in the brine stream pass from the first chamber through a second ion exchange membrane into the third chamber.\|13. The method of claim 12, further comprising:\| directing the aqueous acid solution from an acid buffer tank into said second chamber and directing a first portion of the acid product stream exiting the second chamber to the acid buffer tank;\| directing the aqueous base solution from a base buffer tank into said third chamber and directing a first portion of the base product stream exiting the third chamber to the base buffer tank; and\| directing a portion of the generated freshwater into one or more of said acid buffer tank and said base buffer tank.\|14. The method of claim 8,\| wherein the saltwater feedstock comprises raw seawater obtained from an ocean, and\| wherein the method further comprises:\| generating an ocean alkalinity product using at least a portion of the base product stream such that the ocean alkalinity product includes said base molecules fully dissolved in a salt solution and has a pH level that is a predetermined amount higher than a pH level of the ocean's seawater; and\| supplying the ocean alkalinity product to the ocean at a designated outfall location.\|15. The method of claim 8,\| wherein the saltwater feedstock comprises raw seawater obtained from an ocean, and\| wherein the method further comprises:\| generating an alkaline slurry by combining at least a portion of the base product stream with analkaline aggregate such that a reaction between the alkaline aggregate and the acid molecules both neutralizes the acid molecules and etches the alkaline aggregate; and\| supplying the alkaline slurry to the ocean at a designated outfall location.\|16. A hybrid carbon dioxide removal (CDR) system comprising:\| an ocean alkalinity enhancement (OAE) subsystem including an electrodialysis device configured to electrochemically process salt obtained from an ocean's seawater such that the salt is converted into a base substance and an acid substance, the OAE subsystem further including an alkaline product generator configured to generate an ocean alkalinity product including the base substance fully dissolved in a salt solution;\| an enhanced ocean weathering (EOW) subsystem configured to generate an alkaline slurry by combining a portion of the acid substance from the electrodialysis device with an alkaline aggregate such that an accelerated ocean weathering reaction between the alkaline aggregate and the acid substance both neutralizes the acid substance and etches/weakens the alkaline aggregate; and\| a base delivery subsystem configured to supply the ocean alkalinity product and the alkaline slurry to an ocean such that both the fully dissolved base substance and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification.\|17. The hybrid CDR system of claim 16, wherein the EOW subsystem comprises:\| an accelerated ocean weathering reaction apparatus includes a reaction tank configured to contain a process fluid including a mixture of the alkaline aggregate and acid substance portion until the accelerated ocean weathering reaction is completed; and\| a slurry generator configured to generate the alkaline slurry by processing the etched/weakened alkaline aggregate contained in the process fluid received from the accelerated ocean weathering reaction apparatus.\|18. The hybrid CDR system of claim 17, wherein the slurry generator further is further configured to separate (reclaim) one or more metal elements from the alkaline slurry.\|19. The hybrid CDR system of claim 16, further comprising:\| a mixing device configured to combine a saltwater feedstock stream including the ocean's seawater with the base substance exiting the electrodialysis device to produce a mixture stream; and\| a desalination unit configured to generate a freshwater stream and a brine stream by processing the mixture stream.\|20. The hybrid CDR system of claim 19, wherein electrodialysis device is configured to receive and electrochemically process salt contained in the brine stream.	(US20250339810)\|RELATED APPLICATIONS/PATENTS\|[0001] This application claims priority from U.S. Provisional Patent Application No. 63/716,029, entitled “Integrated Ocean Alkalinity Enhancement And Seawater Desalination”, filed on Nov. 4, 2024, which is entirely incorporated herein by reference.\|[0002] This application also claims priority from U.S. Provisional Patent Application No. 63/641,910, entitled “Electrochemical Assisted Ocean Weathering”, filed on May 2, 2024, which is entirely incorporated herein by reference.\|(US20250339810)\|FIELD OF THE INVENTION\|[0003] The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|BACKGROUND\|[0004] As humans burn more and more fossil fuels, the resulting increased carbon dioxide (CO2) concentration in Earth's atmosphere causes both climate change and ocean acidification. The increased atmospheric concentrations of CO2 and other greenhouse gases (e.g., methane) produces climate change by trapping heat close to earth's surface, thereby increasing both air and sea temperatures. Because earth's oceans absorb about 25% of atmospheric CO2, and because the absorbed CO2 dissolves to form carbonic acid that remains trapped in the seawater, the increased atmospheric CO2 concentration caused by burning fossil fuels also produces ocean acidification by way of increasing the amount of CO2 gas dissolved in the ocean.\|[0005] Both climate change and ocean acidification pose Climate change in the form significant threats to humans. of increased global average temperatures can produce several dangerous effects such as the loss of polar ice and corresponding increased sea levels, disease, wildfires and stronger storms and hurricanes. Ocean acidification changes the ocean chemistry that most marine organisms rely on. One concern with ocean acidification is that the decreased seawater pH can lead to the decreased survival of shellfish and other aquatic life having calcium carbonate shells, as well as some other physiological challenges for marine organisms.\|[0006] To avoid dangerous climate change, the international Paris Agreement aims to limit the increase in global average temperature to no more than 1.5° C. to 2° C. above the temperatures of the pre-industrial era. Global average temperatures have already increased by between 0.8° C. and 1.2° C. The Intergovernmental Panel on Climate Change (IPCC) estimates that a ‘carbon budget’ of about 500 GtCO2 (billion tons of carbon dioxide), which corresponds to about ten years at current emission rates, provides a 66% chance of limiting climate change to 1.5° C.\|[0007] In addition to cutting CO2 emissions by curtailing the use of fossil fuels, climate models predict that a significant deployment of Negative Emissions Technologies (NETs) will be needed to avoid catastrophic ocean acidification and global warming beyond 1.5° C. (see “Biophysical and economic limits to negative CO2 emissions”, Smith P. et al., Nat. Clim. Chang. 2016; 6:42-50). Current atmospheric CO2 and other greenhouse gas concentrations are already at dangerous levels, so even a drastic reduction in greenhouse gas emissions would merely curtail further increases, not reduce atmospheric greenhouse gas concentrations to safe levels. Moreover, the reduction or elimination of certain greenhouse gas sources (e.g., emissions from long-distance airliners) would be extremely disruptive and/or expensive and are therefore unlikely to occur soon.\|[0008] Therefore, there is a need to supplement emission reductions with the deployment of NETs, which are systems/processes that serve to reduce existing atmospheric greenhouse gas concentrations by, for example, capturing/removing CO2 from the air and sequestering it for at least 1,000 years. The need for NETs may be explained using a bathtub analogy in which atmospheric CO2 is represented by water contained in a bathtub, ongoing CO2 emissions are represented by water flowing into the tub, and NETs are represented by processes that control water outflow through the tub's drain. In this analogy, reduced CO2 emission rates are represented by partially turning off the water inflow tap—the slower inflow rate provides more time before the tub fills, but the tub's water level will continue to rise and eventually overflow. Using this analogy, although reducing CO2 emissions may slow the increase of greenhouse gas in the atmosphere, critical concentration levels will eventually be reached unless NETs are implemented that can offset the reduced CO2 emission level (i.e., remove atmospheric CO2 at the same rate it is being emitted). Moreover, because greenhouse gas concentrations are already at dangerous levels (i.e., the tub is already dangerously full), there is an urgent need for NETs that are capable of significantly reducing atmospheric CO2 faster than it is being emitted to achieve safe atmospheric concentration levels (i.e., outflow from the tub's drain must be greater than the reduced inflow from the tap to reduce the tub's water to a safe level).\|[0009] NETs can be broadly characterized as Direct Air Capture (DAC) approaches and Ocean Capture approaches. DAC approaches utilize natural (e.g., reforestation) and technology-based methods to extract CO2 directly from the atmosphere. Ocean capture approaches utilize various natural and/or technological processes to remove CO2 from the atmosphere and store it in the ocean as bicarbonate, a form of carbon storage that is stable for over 10,000 years.\|[0010] Electrochemical ocean alkalinity enhancement (electrochemical OAE or EOAE) represents an especially promising ocean capture approach that both reduces atmospheric CO2 and mitigates ocean acidification by generating an ocean alkalinity product (i.e., an aqueous alkaline solution containing a fully dissolved base substance) and supplying the ocean alkalinity product to ocean seawater at a designated outfall location. Electrochemical OAE systems typically generate the required base substance using an electrochemical reactor referred to as a bipolar electrodialysis device (BPED), which generally includes an electrodialysis (ED) apparatus and associated flow control devices configured to perform an electrochemical salt-conversion process that converts salt supplied in an aqueous salt feedstock solution (e.g., seawater) into the base substance and an acid substance. The base substance produced by the BPED is then incorporated into the ocean alkalinity (base) product that is then supplied to the ocean. As the base substance diffuses (disperses) into the surrounding seawater it serves to directly reverse ocean acidification (i.e., by utilizing the base substance in the ocean alkalinity product to increase the ocean seawater's alkalinity), and indirectly reduces atmospheric CO2 (i.e., increasing the ocean seawater's alkalinity increases the ocean's ability to absorb/capture atmospheric CO2). Moreover, because the generated base substance is fully dissolved in the ocean alkalinity product, the electrochemical OAE approach avoids problems associated with other OAE approaches (e.g., dissolution kinetics issues that are associated with conventional mineral OAE approaches).\|[0011] Although electrochemical OAE approaches show great potential in mankind's efforts to combat global warming and ocean acidification, their widespread acceptance as a suitable NET may be predicated on the continued development of OAE system features that minimize cost per unit of captured/removed atmospheric CO2 (LCOC). For economic reasons related to carbon offsets and trading, NETs having relatively low LCOC ratings are typically favored over NETs exhibiting relatively high LCOCs. When calculating a NET's LCOC rating, many factors are taken into consideration, including capital costs (e.g., construction and installation expenses), and ongoing operating costs (e. g., land, water, maintenance, and electrical power expenses). In the case of OAE systems, the amount of atmospheric carbon removed from the atmosphere over an ocean depends on the amount of base substance supplied to the ocean (i.e., by way of the ocean alkalinity product), whereby the LCOC of an OAE system is predominantly determined by its levelized cost of producing each unit of base substance. In terms of the capital cost components of LCOC, OAE systems have an advantage over many NETs in that OAE systems are relatively inexpensive to construct and install, have a relatively small footprint and can be controlled using automated operating systems. Moreover, due to the high energy consumption and wear-related part replacement costs associated with performing the electrochemical salt-conversion process (described above), the most significant operating costs associated with an OAE system arise in the operation of the OAE system's BPED. Therefore, developments that reduce BPED operating costs arguably provide the most promising way to reduce OAE system LCOC.\|[0012] The BPEDs currently utilized in OAE systems are referred to herein as 3-chamber BPEDs for brevity. Such 3-chamber BPEDs may be characterized by utilizing an electrodialysis apparatus having an ion exchange (IE) stack configured in a 3-chamber cell arrangement, and by utilizing a flow control system capable of directing three different aqueous solutions (i.e., a salt feedstock solution, an acid solution, and a base solution) through corresponding salt/acid/base chambers of the IE stack. The IE stack includes multiple 3-chamber cells arranged in series between opposing electrodes, where each 3-chamber cell includes salt, acid and base chambers that respectively serve as parallel flow channels for the aqueous salt, acid and base solutions as they pass through the IE stack (i.e., each cell includes a salt chamber that channels a portion of the salt feedstock solution, an acid chamber that channels a portion of the aqueous acid solution, and a salt/base chamber that channels a portion of the base solution). Each cell's salt chamber is disposed between and separated from the cell's acid and salt/base chambers by corresponding ion exchange membranes, which are configured to facilitate the transfer of sodium and chloride ions from the salt chamber into the base and acid chambers during the electrochemical process. That is, during the electrochemical process an electric field applied across the IE stack by the electrodes produces an ionic current in a direction perpendicular to the parallel flow paths, whereby anions in the salt/base/acid streams (e.g., chloride ions (Cl−) and hydroxide ions (OH−)) move toward the positive electrode (anode) and cations in the salt/base/acid streams (e.g., sodium ions (Nat) and protons (H+)) move toward the positive electrode (anode). This ionic current causes dissociated salt molecules (i.e., sodium ions (Na+) and chloride ions (Cl−)) to exit the salt feedstock stream in opposite directions (i.e., such that the chloride ions (Cl−) pass through a first ion exchange filter from the cell's salt chamber into the cell's acid chamber, and the sodium ions (Nat) pass through a second ion exchange filter into the acid chamber). The chloride ions (Cl−) then combine with protons (H+) to form “new” acid (HCl) molecules in the acid solution stream passing through each cell's acid chamber, and the sodium ions (Nat) combine with hydroxide ions (OH−) to form “new” base (NaOH) molecules in the base solution stream passing through each cell's salt/base chamber. As a result of this electrochemical salt-conversion process, the base solution exiting the IE stack, which combines the base solution flows exiting each of the cells, has a significantly higher concentration of base substance (e.g., NaOH molecules) than before entering the IE stack. Similarly, the acid solution exiting each cell has a higher concentration of acid substance (e.g., HCl molecules) than before entering the IE stack. That is, the 3-chamber IE stack arrangement is configured such that three separate streams exit the ED apparatus: a reduced-salt solution stream (i.e., having a lower salt content than the salt feedstock solution fed into the ED apparatus), an acid product (strong acid) stream including the “new” acid molecules, and a base product (strong base) stream including the “new” base molecules.\|[0013] The main operational costs associated with 3-chamber BPEDs include the cost of externally supplied electricity and maintenance (e.g., replacement part and manual labor) associated with the IE stack, flow control system and other BPED subsystems required to perform the electrochemical salt-conversion process. A majority of the externally supplied electricity needed to power a given BPED operations is consumed by the IE stack (i.e., to generate the electric field that produces the ionic current) and varies in accordance with the BPED's IE stack arrangement. That is, larger capacity IE stacks (i.e., those capable of generating larger amounts of base substance per hour) typically require a larger number of series-connected cells. Although the salt/acid/base solutions are conductive, each ion exchange membranes functions like a resistor that impedes the applied electric field. Therefore, larger capacity IE stacks require larger amounts of externally supplied electricity to maintain an electric field at a suitably strong level across a larger number of cells (i.e., across a larger number of ion exchange membranes) than that required by smaller capacity IE stacks. Moreover, a significant amount is needed to power the flow control system (e.g., the various pumps and valves required to maintain the pressures and flow rates of the salt/acid/base solution streams) and other BPED subsystems, such as feedstock pretreatment units that are typically utilized to remove solids and other contaminants (e.g., divalent ions) from the aqueous salt feedstock solution (e.g., seawater) in order to reduce fouling (e.g., mineral scaling) in the IE stack. BPED maintenance costs include the cost of replacing parts that periodically wear out during normal BPED operations, costs associated with service/labor required to replace these parts, and costs associated with maintenance-related down-time (i.e., the periods of OAE system non-operation that are required to perform maintenance operations). Similar to the cost of externally supplied electricity, maintenance costs are typically higher for BPEDs with larger capacity IE stacks than BPEDs with lower capacity IE stacks due to the need to periodically replace a greater number of expensive ion exchange membranes and the higher expense associated with the replacement of flow control system and pretreatment unit components capable of the required higher flow capacities. Because the effectiveness of OAE systems as a NET is strongly dependent on minimizing LCOC (i.e., minimizing the levelized cost of producing base substance), and because the cost of externally supplied electricity and maintenance costs (e.g., the cost of ion exchange filters/membrane replacement) represent two of the most significant expenses associated with an OAE system's production of base substance, there is a strong motivation to optimize OAE system operations in a way that minimizes these two cost components.\|[0014] Enhanced ocean weathering (EOW) represents another promising ocean capture approach that both reduces atmospheric CO2 and mitigates ocean acidification. EOW involves spreading finely ground alkaline aggregate (e.g., silicate rock, such as basalt) onto large ocean surface areas. The widely dispersed alkaline aggregate captures large amounts of dissolved CO2 while in contact with the ocean water. The alkaline aggregate then sinks below the surface, thereby storing the captured CO2 in the ocean and slowing ocean acidification by way of direct interaction between the ocean's seawater and the alkaline material. A major challenge faced by EOW technologies is how to maximize CO2 drawdown for a given amount of finely ground alkaline aggregate. Currently, the best strategies for addressing this challenge at scale involve crushing/grinding the alkaline rock into extremely small particles and then dispersing these particles over large areas of the ocean to maximize the ratio of surface area to dispersed volume. A problem with these EOW strategies is that both the crushing/grinding and dispersing processes require a significant amount of energy. As explained above, the effectiveness of EOW systems as a NET is strongly dependent on minimizing LCOC, and because the cost of externally supplied electricity to crush/grind the alkaline rock represents one of the most significant expenses associated with an EOW system, there is a strong motivation to optimize EOW system operations in a way that minimizes this cost component.\|[0015] Seawater desalination is the process of removing salt and other contaminants from seawater, making it suitable for human consumption, irrigation, or industrial uses. Seawater desalination allows coastal communities to use a broader variety of water sources than conventional techniques, improving the resilience of water-stressed communities. Seawater desalination will become increasingly important as climate change threatens traditional water resources. As sea levels rise, existing freshwater aquifers for coastal communities are at an increasingly high risk of seawater intrusion, thereby making seawater desalination an important potential tool to help these communities adjust to climate change.\|[0016] Seawater desalination systems utilize either thermal technologies or membrane-based technologies. Thermal desalination systems heat seawater so that H2O evaporates into steam, leaving behind salt and other impurities, then condenses the steam back into liquid freshwater that is suitable for human consumption or other freshwater uses. Membrane-based desalination describes a class of technologies in which saline water passes through a semi-permeable material that allows H2O through but holds back dissolved solids like salts. Reverse osmosis is the most common membrane-based desalination technology that reverses the natural osmosis process (i.e., the natural movement of freshwater from an area of low salt concentration to an area of high salt concentration) by utilizing high-energy pumps to pressurize seawater located on a first side of a semi-permeable material such that passes through the membrane to generate freshwater (sometimes referred to as permeate) on the opposing (second) side of the membrane and leaving behind high-salt content brine (i.e., aqueous solution having a significantly higher salt content than that of seawater) on the first side of the membrane. Note that the pressure required to force freshwater through a membrane is directly proportional to the feedstock solution's salt content (i.e., saltier water having a relatively high salt concentration requires more pressure than less salty water), but this pressure is limited by the strength of the membrane (i.e., the membrane will rupture if the pressure is too high). Therefore, the strength of the membrane effectively creates an upper limit on the salinity of water that can be treated at a given flow volume, and a feedstock solution having a salt content much higher than seawater typically cannot be purified using reverse osmosis technologies.\|[0017] Problems associated with all seawater desalination technologies are related to the disposition of brine, high operating costs and carbon footprint. Both thermal and membrane-based desalination technologies generate brine having a higher salt concentration than seawater that is typically disposed of by supplying the brine into the ocean in a manner that both avoids ecological hazards (e.g., harm to sea life) and does not increase the salt content of the seawater feedstock drawn into the desalination plant (i.e., significant resources are required to disperse the brine over a large ocean region and far from the seawater feedstock input pipe). In addition, although the most efficient thermal desalination processes typically use more energy than membrane-based approaches, even reverse-osmosis seawater desalination consume large amounts of electrical energy (e.g., to drive seawater feed pumps and to achieve the pressures necessary to force permeate through semi-permeable membranes). This high energy consumption causes conventional seawater desalination plants to have both high operating costs and a large carbon footprint (i.e., due to the significant greenhouse gas emissions associated with the generation of the required electrical energy).\|[0018] What is needed is a system/method that reduces seawater desalination system operating costs (i.e., external electricity and/or maintenance) and greenhouse gas emissions while avoiding the ecological hazards and other problems associated with brine disposition. What is also needed is a carbon dioxide removal (CDR) system/method that minimizes LCOC by way of significantly reducing the operating costs associated with conventional EOAE systems/methods (i.e., external electricity and/or maintenance costs) and/or EOW systems/methods (i.e., crushing/grinding costs).\|SUMMARY OF INVENTION\|[0019] In an embodiment the present invention is directed to a modified desalination process and associated method that utilizes an electrochemical process to both mitigate the above-mentioned brine disposition problem and address other problems associated with conventional desalination systems/methods. Similar to conventional desalination processes, the modified desalination system/method is configured to convert a saltwater feedstock (e.g., brackish groundwater or seawater having an initial/first salt concentration) into a desired stream of freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a byproduct stream containing brine (i.e., saline solution having a relatively high (second) salt concentration that is higher than the initial salt content of the saltwater feedstock). According to an aspect, the modified electrochemical process is utilized to mitigate the above-mentioned brine disposition problem by effectively removing most of the salt from the brine stream in a way that effectively converts the brine stream into a reduced-salt stream having a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. According to another aspect, at least some of the reduced-salt stream generated by the electrochemical process is mixed/combined with the saltwater feedstock (i.e., such that the saltwater feedstock is effectively diluted by the reduced-salt stream before performing the desalination process), thereby reducing freshwater production costs by reducing the amount of salt that must be filtered/removed from the saltwater feedstock during the desalination process (i.e., in comparison to conventional processes in which only saltwater feedstock is desalinated).\|[0020] In an embodiment a modified desalination (or other) system includes an electrochemical reactor (e.g., a bipolar electrodialysis apparatus (BPED)), a mixing device and a desalination unit that are cooperatively coupled and configured to perform the modified desalination process mentioned above. The desalination unit utilizes known techniques to convert a saltwater feedstock having an initial (first) salt concentration into a freshwater stream and a brine stream having a relatively high (second) salt concentration, and the system is configured to direct (e.g., by way of pipes and pumps) the brine stream from an output terminal of the desalination unit to an input terminal of the electrochemical reactor. The electrochemical reactor is configured to channel three separate solutions: an aqueous salt solution that enters the reactor as the brine stream and exits as the reduced-salt stream, an aqueous acid solution that enters as a weak acid stream and exits as an acid product stream, and an aqueous base solution that enters as a weak base stream and exits as a base product stream. The electrochemical reactor is also configured to generate the reduced-salt stream by electrochemically processing the brine stream such that at least some of the salt molecules (e.g., NaCl) contained in the brine stream are converted into acid molecules (HCl) contained in the acid product stream and base molecules (NaOH) contained in a base product stream. According to another aspect, the electrochemical processing is performed at a rate that converts/removes a sufficient amount salt from the salt/saline solution such that the (third) salt concentration of the reduced-salt stream leaving the electrochemical reactor is lower than the initial (first) salt concentration of saltwater feedstock, thereby significantly reducing eco-safety risks and other brine disposition issues associated with conventional desalination systems/processes. According to another aspect, the system is further configured to direct (e.g., by way of pipes and pumps) at least some of the reduced-salt stream from the electrochemical reactor to an input terminal of the mixing device, which is configured to mix a saltwater feedstock stream (i.e., untreated feedstock or treated feedstock) with the reduced-salt stream received from the electrochemical reactor such that the resulting mixture stream has a (fourth) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock, and the desalination unit is configured to generate the freshwater stream and the brine stream by processing the mixture stream (desalination fluid) exiting the mixing device. Mixing (combining) the saltwater feedstock with the reduced-salt stream provides the system with two cost-saving benefits over conventional desalination systems: first, the energy cost required to produce each unit of freshwater is reduced because the amount of raw seawater or briny groundwater that must be pumped from a saltwater feedstock source to the desalination unit is reduced by an amount equal to that of the reduced-salt stream; and second, the operating/maintenance costs of the system are reduced by reducing the amount of salt that must be filtered or otherwise separated from the desalinated fluid (i.e., the feedstock/reduced-salt mixture) by the desalination unit. Accordingly, by utilizing an electrochemical reactor to remove salt from the brine stream generated by the desalination process, and then utilizing the reduced-salt stream generated by the electrochemical reactor to supplement/dilute the saltwater feedstock directed into the desalination unit, the modified desalination system both mitigates the above-mentioned brine disposition problem and addresses other problems associated with conventional desalination systems.\|[0021] In some embodiments, the system includes an optional pretreatment unit that is operably coupled between a saltwater feedstock source (e.g., ocean or well) and the mixing device, and is configured to remove solids and other contaminants from a stream (portion) of “raw” saltwater feedstock that has been pumped or otherwise delivered from the saltwater feedstock source (e.g., seawater pumped directly from an ocean or briny groundwater pumped from a well), and is further configured to deliver the resulting treated saltwater feedstock to the mixing device by way of the saltwater feedstock stream. In some embodiments the pretreatment unit includes filtering systems or other devices that function to remove solids and at least some contaminants (e.g., biological material and/or divalent ions) from the received raw saltwater feedstock. In an exemplary embodiment, the pretreatment unit includes one or more series connected filtering devices that utilize associated filters to remove contaminants from raw saltwater feedstock (e.g., a first filtering system that utilizes first filter(s) to remove solid particles from seawater, and a second filtering system that utilizes second filter(s) to selectively remove metals and/or biologic materials of value from the partially filtered seawater/brine received from the first filtering system). The filtered contaminants (e.g. removed solids, metals and/or biological materials) are removed from the feedstock flow path using known techniques, and the resulting treated (filtered) feedstock solution (i.e., the treated saltwater feedstock solution that has passed through the filters) forms the saltwater feedstock stream that is passed downstream to the mixing device for mixing with the reduced-salt stream received from the electrochemical reactor). In another exemplary embodiment, the pretreatment unit includes nanofiltration, ultrafiltration, chemical precipitation or other water purification system(s) that is/are configured to remove contaminants and reduce the hardness of the saltwater feedstock by filtering/removing dissolved metal ions and other hardness related minerals (e.g., calcium (Ca2+), magnesium (Mg2+), carbonate (CO3)2−, and iron (Fe2+/Fe3+)), and the system may be configured to return the filtered/removed hardness related minerals to the ocean by way of the ocean alkalinity product. Utilizing the pretreatment unit further reduces operating and maintenance costs by extending the uninterrupted operating period of the desalination unit. Moreover, because the reduced-salt stream is utilized as described above to reduce the required amount of raw saltwater feedstock, the cost of maintaining pretreatment units is lower than that of conventional desalination systems (i.e., reducing the amount of saltwater feedstock passed through the pretreatment unit reduces the rate of filter replacement or other periodic maintenance). In some embodiments a second ion removal process (e.g., filtering similar to that used to remove harness related minerals) is applied to the byproduct brine stream leaving the desalination unit (i.e., before the brine stream is supplied to the electrochemical reactor 110E), thereby further reducing operating costs. In other embodiments, the pretreatment unit may be omitted, for example, in cases where the raw saltwater feedstock is sufficiently free of contaminants when delivered to the desalination system.\|[0022] In some embodiments, the mixing device is configured to generate the mixture stream supplied to the desalination unit at a constant outflow rate by combining all of the reduced-salt stream received from the electrochemical reactor with a corresponding portion of the treated/untreated saltwater feedstock. As mentioned above, the salt content of the mixture stream exiting the mixing device is inversely proportional to the respective inflow rates of the reduced-salt stream and the saltwater feedstock, so minimizing the mixture stream's salt content (and thus minimizing desalination operating/maintenance costs) involves admitting as much of the reduced-salt stream as possible into the mixing device. In cases where the outflow rate of the mixture stream is determined by the combined reduced-salt stream and saltwater feedstock inflow rates, and is maintained constant (e.g., at the maximum processing rate of the desalination unit), the constant mixture stream outflow rate is achieved by admitting the total amount/inflow of the reduced-salt stream delivered to the mixing device and the controlling (i.e., increasing or decreasing) the saltwater feedstock inflow rate such that the combined inflow rates equal the constant mixture stream outflow rate. In some embodiments, a sensor monitors the flow rate of the reduced-salt stream delivered to the mixing device and a feedstock flow control device is utilized to control a (first) inflow rate of the saltwater feedstock stream into the mixing device, where the system controller controls the feedstock flow control device such that the (first) inflow rate is adjusted (increased/decreased) in accordance with changes (decreases/increases) in the (second) inflow rate of the reduced-salt stream into the mixing device. In some embodiments, the mixing device includes a mixing tank that receives the reduced-salt stream exiting the ED apparatus and a treated saltwater feedstock stream exiting a pretreatment unit such that the two streams intermix within the tank to form the mixture stream. In other embodiments, the mixing device may be implemented, for example, using interconnecting pipes or other mixing structures.\|[0023] As set forth above, the desalination unit functions to desalinate the mixture stream received from the mixing device to generate freshwater and the high-salt brine/feedstock stream. In some embodiments, the desalination unit utilizes a known desalination device/process (e.g., thermal desalination or membrane-based desalination) to separate the mixture stream into the desired freshwater (permeate) stream and the byproduct brine stream. In an exemplary embodiment, the desalination unit utilizes a reverse osmosis (RO) system including a semi-permeable membrane that prevents the passage of salt molecules, whereby the brine stream is formed on one side of the membrane and permeate (freshwater) passes to the opposing side of the membrane. Similar to conventional desalination processes, the freshwater generated by the desalination unit has a suitably low salt concentration (e. g., ≤500 ppm), and the brine stream comprises an aqueous solution having salt content greater than 50,000 ppm (5%).\|[0024] In an embodiment the electrochemical reactor is implemented using a bipolar electrodialysis system (BPED) of a type similar to that utilized in existing OAE systems to convert the high-salt brine stream into the reduced-salt stream. The BPED includes an electrodialysis (ED) apparatus that utilizes an ion exchange stack to perform an electrochemical salt-conversion process during which salt supplied in the brine stream is converted into a base substance and an acid substance. In some embodiments, the ion exchange stack comprising a series of salt chambers, acid chambers and base chambers that are arranged in series between opposing electrodes, where each salt chamber is located between and separated from associated pair of adjacent acid and base chambers by an associated intervening ion exchange membrane. The BPED also includes a flow control system including a first portion that is configured to direct the brine stream through the salt chambers of the ion exchange stack, a second portion configured to direct an aqueous acid solution through the acid chambers and a third portion configured to direct an aqueous base solution through the base chambers. During operation the opposing electrodes apply an electric field across the ion exchange stack to electrochemically process salt (e.g., NaCl) in the brine stream disposed in each salt chamber such that chlorine ions (Cl−) pass through first ion exchange membranes and combine with dissociated protons (H+) to form “new” acid molecules (HCl) in the aqueous acid solution disposed in the associated adjacent acid chamber, and such that sodium ions (Na+) pass through second ion exchange membranes and combine with dissociated hydroxide ions (OH−) to form “new” base molecules (NaOH) in the aqueous base solution disposed in the associated adjacent base chamber. In this manner, the electrochemical process causes the acid and base product streams leaving the ED apparatus to have a higher acid and base concentrations, respectively, than the acid/base solutions entering the ED apparatus. Conversely, the electrochemical process causes the reduction (removal) of salt from the brine solution passed through the ED apparatus, whereby the reduced-salt solution stream exiting the ED apparatus has a salt concentration that is substantially lower than that of the brine stream entering the ED apparatus. By utilizing a BPED similar to those used in stand-alone OAE systems (or another electrochemical reactor having a similar salt processing capacity), the reduced-salt solution can be generated with a salt concentration that is equal to or lower than that of seawater (e.g., below 35,000 ppm (3.5%)), thereby addressing the brine disposition issues associated with stand-alone desalination plants.\|[0025] In some embodiments, the electrochemical reactor also includes a fluid buffering system including an acid buffer tank and a base buffer tank that facilitate the circulation of the aqueous acid and base solutions through the ED apparatus. Specifically, the acid buffer tank is configured to contain the aqueous acid solution that is directed (by way of associated flow control elements) into the acid (second) chamber(s) of the ion exchange stack and to receive a first portion of the acid product stream exiting (directed away from) the acid chambers(s). Similarly, the base buffer tank is configured to contain the aqueous base solution that is directed to the base (third) chamber(s) of the ion exchange stack and to receive a first portion of the base product stream exiting the base chamber(s). Note that second portions of the acid and base product streams are typically diverted for other purposes (e. g., maintenance, OAE or commercial sale). As mentioned above, the electrochemical reactor's flow control system is configured such that the brine stream exiting the desalination unit is directed to the ED apparatus, and at least a portion of the reduced-salt stream exiting the ED apparatus is directed to the mixing device. This salt solution flow arrangement differs from BPEDs utilized in conventional OAE systems in which the reduced/depleted salt stream exiting an ED apparatus is typically utilized to replenish (make up) any acid/base product diverted from the electrochemical reactor for other purposes and to control the acid/base concentration (dilution) of the weak acid and base solutions directed to the ED apparatus. To facilitate dilution of the acid and/or solution streams in cases where all of the reduced-salt stream is directed to the mixing device, in one embodiment, the flow control system is further configured to divert some of the freshwater stream exiting the desalination unit such that it flows into the acid buffer tank and/or the base buffer tank. Although utilizing some of the freshwater for acid and/or base dilution reduces the amount of freshwater output from the system, the required dilution amount is typically much less than that produced by the desalination unit, and may provide a net benefit, for example, in cases where high quality acid product is desired (i.e., the acid product's value is typically inversely proportional to the amount of salt in the acid solution). In other embodiments, replenishing for the acid and/or base product streams may be achieved using a portion of the reduced-salt stream or using a mixture of both freshwater and reduced-salt streams.\|[0026] In some embodiments the brine stream exiting the desalination unit may be passed directly to the ED apparatus (i.e., the fluid buffer system may only include an acid buffer tank and a base buffer tank, and omit a salt buffer tank). In other embodiments, the fluid buffer system may include a salt buffer tank that is operably coupled between the desalination unit and the ED apparatus, and serves as a buffer for aqueous salt solution (i.e., such that a portion of the brine stream produced by the desalination unit is stored in the salt buffer tank). In this case, the salt buffer tank may be used to regulate the flow rate of brine into the ED apparatus.\|[0027] In some embodiments, the electrochemical reactor is configured to process brine at a rate that corresponds with a desired maximum freshwater production rate. That is, a desalination unit that is capable of generating freshwater at a relatively high flow rate also generates brine at a relatively high flow rate, so, to avoid the buildup of unprocessed brine, the electrochemical reactor must be capable of converting the brine stream into a corresponding reduced-salt stream at a corresponding flow rate. In addition to suitable flow control and buffer resources, the electrochemical reactor's ED apparatus must be configured to receive and process brine at the corresponding flow rate, for example, by way of providing a sufficient number of cells (i.e., groups of salt, acid and base chambers separated by intervening ion exchange membranes) arranged in series between suitable electrodes, and otherwise configuring the ED apparatus to facilitate the conversion of brine at the relatively high flow rate.\|[0028] In another exemplary embodiment, an integrated (combined) desalination/OAE system includes a seawater desalination subsystem and an OAE subsystem (electrochemical reactor). The seawater desalination subsystem generates a freshwater stream by desalinating seawater pumped or otherwise drawn from a nearby ocean using any of the desalination processes mentioned above. The OAE subsystem includes an ED apparatus that converts salt provided in the byproduct brine stream from the desalination process into acid and base product streams. The system also includes a post-production unit that selectively utilizes a portion of the base product stream to generate an ocean alkalinity product and selectively utilizes a portion of the acid product stream to generate an alkaline slurry, and then supplies (e.g., pumps) the ocean alkalinity product and the alkaline slurry to the ocean at a designated outfall location for OAE and enhanced ocean weathering (EOW) purposes (i.e., such that both the fully dissolved base substance in the ocean alkalinity product and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification). Integrating seawater desalination and at least one of OAE or EOW operations in the manner set forth herein essentially eliminates the ecological concerns associated with conventional stand-alone seawater desalination and significantly decreases total operating costs (i.e., in comparison with conventional stand-alone seawater desalination). That is, because the brine stream has a higher salt concentration than seawater, electrochemically processing the brine stream (i.e., in place of seawater) enhances the generation of ocean alkalinity product by decreasing the amount of externally supplied energy that is required to perform the electrochemical conversion of salt molecules (e.g., NaCl) into acid molecules (e.g., HCl) and base molecules (e.g., NaOH) for a given flow rate through the electrochemical reactor, thereby increasing the base product production efficiency and decreasing total operating cost over conventional stand-alone OAE systems that process seawater, thereby reducing LCOC in comparison to such OAE systems. Moreover, by generating and supplying alkaline ocean product and alkaline slurry to the ocean, the resulting OAE effectively offsets the carbon footprint of the seawater desalination process, and the integrated desalination/OAE system achieves greatly reduces total operating costs over separate (stand-alone) desalination and OAE plants. In addition, utilizing the reduced-salt stream, which is generated as a byproduct of the OAE process, to supplement the seawater (saltwater feedstock) processed by the desalination subsystem reduces operation and maintenance costs over conventional stand-alone seawater desalination plants, for example, by reducing the amount of raw seawater that must be pumped from an ocean and pretreated before desalination. Further, utilizing an electrochemical reactor to process the brine stream that is generated as a byproduct of the desalination process provides additional advantages including: (1) reducing environmental issues and dispersion costs associated with releasing high-salt-content brine directly from the desalination process into an ocean; and (2) reduces maintenance costs by facilitating the use of the generated acid product (e.g., HCl), e.g., to clean semi-permeable and/or ion exchange membranes utilized in the ion exchange stack. Moreover, integrating seawater desalination and OAE subsystems facilitates other benefits such as capital expense reductions achieved by shared plant facilities (e.g., project site and shelter/building), shared saltwater feedstock intake/outfall structures and associated operating costs, shared water treatment operating costs, and shared electrical infrastructure. Further, permitting (government authorization) for desalination plants is difficult in some regions because of eco-safety risks that are primarily due to the increased salinity of the outfall brine—the present invention mitigates this eco-safety risk by utilizing an electrochemical reactor to process the brine such that its final salinity is closer to ambient conditions, thereby leading to an easier permitting process for desalination plants modified in the manner described herein.\|[0029] Although described herein with specific reference to specific modified desalination and integrated desalination/OAE/EOW systems/methods, the present invention may also be utilized to provide other commercially advantageous operations that may achieve at least some of the benefits set forth above. For example, the base product and/or acid product generated by the electrochemical reactor/process may be selectively utilized for non-OAE uses. Although the carbon footprint of the resulting desalination system/process may be higher than that of the combined desalination/OAE approach, the desalination system/process would still have advantages over conventional seawater desalination operations. That is, utilizing the electrochemical reactor to reduce the salt content of the high-salt brine/feedstock stream significantly reduces eco-safety risks and other issues associated with the disposition of the high-salt brine generated by conventional desalination processes. In an exemplary embodiment, the system's controller may monitor one or more sites that provide input data including spot pricing for the base product and/or acid product generated by the electrochemical reactor. The controller may then utilize this input data to determine whether the base and/or acid products should be utilized for OAE/EOW purposes, or whether they should be sold to a third-party buyer. For example, when sufficient low/zero-carbon electricity is available from a power grid to offset the desalination process carbon footprint and the base product spot price is sufficiently high, then the controller may direct the post-production unit to divert the base product (e.g., some or all of the second base stream portion) for sale to a third-party buyer (i.e., instead of directing the base product to the ocean as part of ocean alkalinity product), whereby proceeds from the sale serve to reduce total operating costs of the system. Similarly, the control algorithm implemented by the system's controller may monitor input data from one or more sites that provide spot pricing for the acid product (e.g., HCl) generated by the electrochemical reactor, and utilizes this data to determine whether it is more cost effective to neutralize the acid product (e.g., by way of enhanced ocean weathering), or if selling the acid product may produce a greater value (i.e., if the acid product spot price is sufficiently high), in which case the controller may direct the post-production unit to divert the acid product (e.g., some or all of the second acid stream portion) for sale to a third-party buyer.\|[0030] According to another embodiment, a hybrid carbon dioxide removal (CDR) system includes an electrochemical OAE subsystem configured to generate an ocean alkalinity product, an EOW subsystem configured to generate an alkaline slurry, and a base delivery subsystem configured to supply at least one of the ocean alkalinity product and the alkaline slurry to an ocean to capture/reduce atmospheric carbon dioxide and mitigate ocean acidification. The electrochemical OAE subsystem utilizes an ED device configured to electrochemically process/convert salt into an acid substance and base substance and utilizes an alkaline product generator to generate an ocean alkalinity product including the base substance. In an exemplary embodiment, the EOW subsystem includes an accelerated ocean weathering reaction apparatus and a slurry generator. The accelerated ocean weathering reaction apparatus is configured to combine the acid substance from the electrodialysis device with an alkaline aggregate such that an accelerated ocean weathering reaction between the alkaline aggregate and the acid substance both neutralizes the acid substance and etches/weakens the alkaline aggregate. The slurry generator then receives the neutralized (fully processed) process fluid exiting the reaction apparatus and processes the etched/weakened alkaline aggregate into fine particles, thereby forming the alkaline slurry. In some embodiments, metal elements are released from the alkaline aggregate during the accelerated weathering and slurry generation processes and are reclaimed from the alkaline slurry to offset operating costs. The base delivery subsystem is configured to supply at least one of the ocean alkalinity product and the alkaline slurry to the ocean. By utilizing the acid substance of the electrochemical process to etch/weaken the alkaline aggregate, the accelerated (electrochemically assisted) ocean weathering process implemented by the EOW subsystem produces alkaline slurry at a significantly reduced cost in comparison to conventional EOW systems. That is, the acid substance, which is a byproduct of the electrochemical process and is therefore essentially cost free, serves to etch/weaken the alkaline aggregate, thereby increasing the etched/weakened aggregate's specific surface area and/or facilitating crushing/grinding the etched/weakened aggregate into alkaline particles suitable for ocean dispersal offsetting energy than would be required by conventional EOW crushing/grinding operations. Moreover, during the accelerated weathering operation the alkaline material in the alkaline aggregate neutralizes the acid substance, thereby circumventing acid storage/neutralization issues associated with conventional OAE technologies. Further, by supplying both the electrochemically generated ocean alkalinity product and the alkaline slurry to the ocean, the hybrid CDR system achieves at least the same amount of carbon capture removal and ocean deacidification as that achieved by independently operated conventional OAE and EOW systems using significantly less energy than separate conventional OAE and EOW systems. In some embodiments the CDR system utilizes a desalination subsystem to convert seawater from the ocean into a high-salt-content brine in order to enhance the electrochemical process.\|(US20250339810)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0031] FIG. 1 shows a modified desalination system according to an exemplary embodiment of the present invention;\|[0032] FIG. 2 shows a simplified electrochemical reactor that may be utilized to electrochemically process a brine solution in the modified desalination system of FIG. 1, according to an exemplary specific embodiment;\|[0033] FIG. 3 shows a simplified electrodialysis apparatus that may be utilized by the electrochemical reactor of FIG. 2 to electrochemically convert salt into acid and base products according to another exemplary embodiment;\|[0034] FIG. 4 shows a modified desalination system according to another exemplary embodiment; and\|[0035] FIG. 5 shows an integrated desalination/OAE/EOW system according to another exemplary embodiment of the present invention; and\|[0036] FIG. 6 shows an EOW subsystem of the integrated desalination/OAE/EOW system of FIG. 5 in additional detail according to an exemplary embodiment.\|(US20250339810)\|DETAILED DESCRIPTION\|[0037] The present invention combines desalination and electrochemical systems/processes in a way that converts a saltwater feedstock (e.g., seawater or briny groundwater) into freshwater suitable for human consumption and other freshwater uses, a base substance suitable for OAE purposes, and an acid substance. The invention is primarily described herein with specific reference to a modified desalination system/method that utilizes a desalination subsystem/process to convert saltwater feedstock into freshwater and brine and utilizes an electrochemical reactor/process to convert the brine into a reduced salt solution (i.e., by converting salt in the brine into acid and base substances). In one embodiment, the invention is described with reference to an integrated desalination/OAE/EOW system/method that desalinates seawater to produces freshwater and brine, electrochemically processes the brine to generate acid and base products, utilizes the base product to perform an OAE process, and utilizes the acid product to reduce the energy costs associated with crushing/grinding alkaline aggregate in an EOW process. However, in some embodiments, the systems/methods described herein may be utilized for other purposes, including a stand-alone hybrid HDR system/method or a system/method for generating acid and/or base substances in remote locations. The following description is presented to enable one of ordinary skill in the art to make and use the methods and systems described herein as provided in the context of specific embodiments. Various modifications to the embodiments will be apparent to those with skill in the art, and the general principles defined herein may be applied to other embodiments. Therefore, the methods and systems described herein are not intended to be limited to the particular embodiments shown and described, but are to be accorded the widest scope consistent with the principles and novel features herein disclosed.\|[0038] FIG. 1 depicts a modified desalination system 100 including an electrochemical reactor 110, a desalination subsystem 160 and a system controller 190. Electrochemical reactor 110 performs an electrochemical process in which a high-salt-content brine stream 111-1 is received from the desalination subsystem 160, salt contained in brine stream 111-1 is electrochemically processed (removed), and then at least a portion 111-21 of the resulting reduced-salt stream 111-2 is directed back to desalination subsystem 160. Desalination subsystem 160 performs a modified desalination process in which a mixing device 170 mixes (combines) a saltwater feedstock stream 51T (e.g., seawater or briny groundwater) with reduced-salt stream portion 111-21 received from electrochemical reactor 110 to form a mixture stream 51M, and then a desalination unit 180 processes (desalinates) mixture stream 51M to generate a freshwater stream 115 (i.e., water suitable for human consumption, irrigation, or industrial uses) and brine stream 111-1, which is directed to electrochemical reactor 110. System controller 190 controls the various operations performed by electrochemical reactor 110 and desalination subsystem 160 such that at least a portion of freshwater 115 exiting desalination subsystem 160 is directed out of system 100 as freshwater output stream 115-OUT for fresh water uses. Additional details regarding the various components and processes of system 100 are set forth below.\|[0039] Referring to the left side of FIG. 1, desalination subsystem 160 includes an optional pretreatment unit 165, a mixing device 170 and a desalination unit 180 that process saltwater feedstock 51 to generate freshwater stream 115 and brine stream 111-1.\|[0040] Optional pretreatment unit 165 is configured to treat a “raw” saltwater feedstock stream 51 (i.e., feedstock received directly from an external source, such as raw seawater pumped from an ocean 50, or briny groundwater pumped from a well) by removing (e.g., filtering) solids and other contaminants (e.g., biological material and/or divalent ions) from the raw feedstock. The resulting treated saltwater feedstock exiting pretreatment unit 165 is then supplied to mixing device 170 as saltwater feedstock stream 51T. Note that optional pretreatment unit 165 does not significantly reduce or otherwise change the salt content of the saltwater feedstock (i.e., the treated saltwater forming saltwater feedstock stream 51T has substantially the same initial (first) salt concentration as the raw saltwater forming feedstock stream 51. Pretreatment unit 165 may be omitted, for example, is cases where raw saltwater feedstock stream 51 is sufficiently pure (i.e., free of contaminants), or in embodiments where the raw saltwater feedstock is treated prior to being delivered into desalination subsystem 160. When pretreatment unit 165 is omitted, raw saltwater feedstock is passed directly to mixing device 170 (i.e., saltwater feedstock stream 51T and raw saltwater feedstock stream 51 comprise the same saltwater feedstock stream).\|[0041] Mixing device 170 is configured to receive reduced-salt stream portion 111-21 from electrochemical reactor 110 (i.e., some or all of reduced-salt stream 111-2 exiting ED apparatus 130) and saltwater feedstock stream 51T from pretreatment unit 165. Mixing device 170 utilizes one or more mechanisms (e.g., a mixing tank and/or pumps) to mix (combine) the two streams and to produce a mixture stream 51M including a mixture solution having a (fourth) salt concentration that is between the initial (first) salt concentration of saltwater feedstock stream 51T and an intermediate (third) salt concentration of the reduced-salt stream 111-21. As described in additional detail below, electrochemical reactor 110 is configured to generate reduced-salt stream 111-2 such that the intermediate (third) salt concentration is lower than the initial (first) salt concentration of saltwater feedstock stream 51T. Therefore, mixture stream 51M comprises an aqueous solution having a salt concentration that is lower than the initial salt concentration of the saltwater feedstock. An outlet of mixing device 170 is operably coupled to an inlet of desalination unit 180 such that mixture stream 51M is directed into desalination unit 180. In some embodiments (not shown), the mixing process performed by mixing device 170 may be implemented by either optional pretreatment unit 165 or desalination unit 180.\|[0042] In some embodiments mixing device 170 is configured to generate mixture stream 51M by combining all of reduced-salt stream 111-21 received from electrochemical reactor 110 with a corresponding portion of the treated/untreated saltwater feedstock included in saltwater feedstock stream 51T. That is, the flow rate of mixture stream 51M exiting mixing device 170 is substantially equal to a sum of the inflow rate of reduced-salt stream 111-21 received from electrochemical reactor 110 and the inflow rate of saltwater feedstock stream 51T. In this preferred embodiment, mixture stream 51M includes the total amount of reduced-salt stream 111-21 received from electrochemical reactor 110 and adjusts, if necessary, the inflow rate of saltwater feedstock stream 51T (e.g., by way of a feedstock flow control device 171). For example, assuming desalination unit 180 is configured to process mixture stream 51M at a total flow rate of 100 units per minute, if electrochemical reactor 110 provides reduced-salt stream 111-21 to mixing device 170 at an inflow rate of 30 units/min then the corresponding inflow rate of saltwater feedstock stream 51T is adjusted to equal 70 units/min, and if electrochemical reactor 110 subsequently provides reduced-salt stream 111-21 at an inflow rate of 35 units/min then the corresponding inflow rate of saltwater feedstock stream 51T is adjusted to 65 units/min. Utilizing all of the available reduced-salt stream 111-21 to generate mixture stream 51M minimizes the amount of salt that must be removed from mixture stream 51M by desalination unit 180 (i.e., by minimizing the proportion of saltwater feedstock to reduced-salt solution in mixture stream 51M). Note that variations in the inflow rate of reduced-salt stream 111-21 may occur for purposes of project wide optimization. For example, when acid production is valued higher than freshwater and base production, then freshwater stream portion 115-2 may be directed to acid buffer tank 121-2 (i.e., to increase the value of acid product stream 112-2 by minimizing salt content), whereby more of reduced-salt stream 111-2 may be directed to mixing device 170 as reduced-salt stream portion 111-21. In other cases it may be determined that freshwater and/or base production may be optimized when both freshwater stream portion 115-2 and reduced-salt stream 111-22 are simultaneously directed to acid buffer tank 121-2 and/or base buffer tank 121-3, where the system controller adjusts the fractions of the freshwater and reduced-salt streams to optimize the salt content in the acid and base solutions. In other embodiments, system optimization may be achieved by replenishing (making-up) for the acid product stream 112-22 and/or base product stream 113-22 using only reduced-salt stream portion 111-22 with the remainder of reduced-salt stream 111-2 being directed to mixing device 170 as reduced-salt stream portion 111-21. Whenever system optimization requires a corresponding change (increase/decrease) in the inflow rate of salt stream portion 111-21 to mixing device 170, the system controller makes a corresponding adjustment (decrease/increase) to the inflow rate of saltwater feedstock stream 51T so that the outflow rate of mixture stream 51M remains constant.\|[0043] Desalination unit 180 is configured to perform a desalination process on mixture stream 51M in a manner that generates high-salt brine stream 111-1, which is then directed to electrochemical reactor 130, and freshwater stream 115 comprising water having a salt concentration that is suitable for human consumption (e.g., less than or equal to 0.05% (≤500 ppm). By way of example, when the saltwater feedstock comprises seawater pumped from an ocean, saltwater feedstock stream 51/51T has a salt concentration of about 3.5%, the relatively high salt concentration of brine stream 111-1 may be greater than 5%. As described in additional detail below, in alternative embodiments desalination unit 180 may be implemented using a thermal desalination system, a reverse osmosis system or another membrane-based (or other) desalination system.\|[0044] Referring to the right side of FIG. 1, electrochemical reactor 110 includes a fluid buffering system 120, an electrochemical reactor 130 and a flow control system. As set forth in additional detail below, electrochemical reactor 110 is configured to generate reduced-salt stream 111-2 by electrochemically processing the brine stream 111-1 such that at least some of the salt molecules (e.g., NaCl) contained in brine stream 111-1 are converted into acid molecules (e.g., HCl) contained in an acid product stream 112-2 and base molecules (NaOH) contained in a base product stream 113-2, and such that the reduced-salt stream 111-2 exiting the electrochemical reactor 110 has a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. Note that electrochemical reactor 110 is greatly simplified for descriptive purposes, and that additional details regarding its construction and operation are provided below with reference to the exemplary embodiments depicted in FIGS. 2 to 5.\|[0045] Fluid buffering system 120 includes an acid buffer tank (ABT) 121-2 and a base buffer tank 121-3. Acid buffer tank 121-2 is configured to contain an aqueous acid solution that is circulated through reactor 130 by way of associated flow control structures (e.g., pipes and pumps) such that a relatively weak acid stream 112-1 is directed from acid buffer tank 121-2 to reactor 130 and at least a portion 112-21 of a relatively strong acid product stream 112-2 leaving reactor 130 is directed back to acid buffer tank 121-2. Base buffer tank 121-3 is configured to contain an aqueous base solution that is circulated through reactor 130 by way of associated flow control structures such that a relatively weak base stream 113-1 is directed from base buffer tank 121-3 to reactor 130 and at least a portion 113-21 of a relatively strong base product stream 113-2 leaving reactor 130 is directed back to base buffer tank 121-3. In some embodiments, the flow control system is further configured to direct a portion 115-2 of freshwater 115 into one or more of acid buffer tank 121-2 and base buffer tank 121-3 to dilute the weak solutions directed into reactor 130.\|[0046] ED apparatus 130 generally includes an ion exchange (IE) stack 135 that is disposed between two electrodes (i.e., anode 138+ and cathode 138−). IE stack 135 typically includes multiple cells arranged in series between electrodes 138+ and 138−, where each cell includes three chambers that respectively serve as parallel flow channels for the aqueous salt, acid and base solutions as they pass through IE stack 135. For brevity and clarity, only one cell of IE 135 is depicted in FIG. 1, which is made up of a salt chamber 131 that functions to channel a portion of the aqueous salt solution, an acid chamber 132 that channels a portion of the aqueous acid solution, and a base chamber 133 that channels a portion of the aqueous base solution. Each cell's salt chamber 131 is disposed between and separated from the cell's acid chamber 132 and base chamber 133 by corresponding ion exchange membranes 134-1 and 134-2, which are configured to facilitate the transfer of sodium and chloride ions from the salt chamber into the base and acid chambers during the electrochemical process as described below. ED apparatus 130 also includes manifold or other structures (not shown) that are configured to cooperate with the flow control resources of BPED 110 to direct the three different (i.e., a salt, acid and base) aqueous solutions through corresponding salt/acid/base chambers of IE stack 135. Specifically, the aqueous salt solution enters IE stack 135 as brine stream 111-1 that is divided and directed (e.g., by an input manifold, not shown) into the inlet of each cell's salt flow channel 131, and the aqueous salt solution exits the IE stack 135 by way of an outlet of each cell's salt flow channel 131 (and an outlet manifold, not shown) as reduced-salt stream 111-2. Similarly, the aqueous acid solution enters IE stack 135 as a weak acid stream 112-1 that is directed into the inlet of each cell's acid flow channel 132 and exits the IE stack 135 by way of an outlet of each cell's acid flow channel 132 as acid product stream 112-2. Finally, the aqueous base solution enters IE stack 135 as a weak base stream 113-1 that is directed into the inlet of each cell's base flow channel 133 and exits the IE stack 135 by way of an outlet of each cell's base flow channel 133 as base product stream 113-2.\|[0047] During the electrochemical process the three (salt, acid and base) aqueous solutions are directed through IE stack 135 along parallel flow paths (e.g., in the vertical direction) while a stack voltage VSTACK is applied to electrodes 138+ and 138−. When stack voltage VSTACK is sufficiently strong, the resulting electric field E produces an ionic current across IE stack 135 in a direction perpendicular to the parallel flow paths (e.g., in the horizontal direction). This ionic current causes dissociated salt molecules (i.e., sodium ions (Na+) and chloride ions (Cl−)) to exit brine stream 111-1 in opposite directions (i.e., such that the chloride ions (Cl−) pass through ion exchange filter 138-1 from salt chamber 131 into the acid chamber 132, and the sodium ions (Nat) pass through ion exchange filter 138-2 into base chamber 133). The chloride ions (Cl−) then combine with protons (H+) to form “new” acid molecules (HCl) in the acid solution stream flowing through acid chamber 132, and the sodium ions (Na+) combine with hydroxide ions (OH−) to form “new” base molecules (NaOH) in the base solution stream flowing through base chamber 133. As a result of this electrochemical salt-conversion process, base product stream 113-2 exits each cell's base chamber 133 with a significantly higher concentration of base molecules than weak base stream 113-1 (i.e., the aqueous base solution before it enters IE stack 135). Similarly, acid product stream 112-2 exiting each cell's acid chamber 132 has a higher concentration of acid molecules than that of weak acid stream 112-1. Note that, because salt is converted (consumed) to generate the acid and base molecules, reduced-salt stream 111-2 exiting each cell's salt chamber 131 has a lower salt concentration than inflowing brine stream 111-1.\|[0048] Referring to the lower left portion of FIG. 1, system controller 190 controls the various operations performed by electrochemical reactor 110 by way of operation/control signals 191, and controls the various operations performed by desalination subsystem 160 way of operation/control signals 192 such that at least a portion of the freshwater 115 exiting desalination unit 180 is directed out of system 100 as freshwater output stream 115-OUT. In an embodiment system controller 190 controls the operating state of ED apparatus 130 such that the above-described electrochemical process is performed at a rate that converts/removes a sufficient amount salt from brine stream 111-1 such that reduced-salt stream 111-2 leaving electrochemical reactor 110 has a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. In some embodiments system controller 190 controls a flow rate of mixture stream 51M into desalination unit 180 using sensor data from sensors configured to measure the flow rate of reduced-salt stream portion 111-21 (i.e., some or all of reduced-salt stream 111-2) from electrochemical reactor 110 into mixing device 170 and using a feedstock flow control device (e.g., pump or valve) to control the associated flow rate of saltwater feedstock stream 51T into mixing device 170. Note that, because the salt concentration of reduced-salt stream 111-2 is lower than the initial (first) salt concentration of saltwater feedstock 51/51T, any non-zero flow rate of reduced-salt stream portion 111-21 into mixing device 170 causes the solution forming mixture stream 51M to have a (fourth) salt concentration that is lower than the initial (first) salt concentration of saltwater feedstock 51/51T. Therefore, although operational and maintenance costs associated with desalination subsystem 160 may be reduced by way of directing all (i.e., the totality of) reduced-salt stream 111-2 from ED apparatus 130 to mixing device 170, beneficial reductions in total system operating costs may be achieved when reduced-salt stream portion 111-21 includes less than all of reduced-salt stream 111-2, and the remaining portion is redirected for other purposes (e.g., reduced-salt stream portion 111-22 may be used in place of or in combination with freshwater portion 115-2 to replenish (make-up) the acid and base solutions stored in buffer tanks 121-2 and 121-3). In some embodiments, system controller 190 is implemented using one or more processors configured to implement a software-based control algorithm that utilizes one of a proportional integral derivative, machine learning and/or artificial intelligence to coordinate the desalination and OAE processes (described below). In some embodiments, controller 190 controls the operations performed by electrochemical reactor 110 to perform additional functions described in co-owned U.S. Pat. No. 11,629,067, cited above.\|[0049] FIG. 2 shows a generalized bipolar electrodialysis (BPED) system (electrochemical reactor) 110A of a type similar to that utilized in some Ocean alkalinity enhancement (OAE) systems. BPED 110A generally includes a fluid buffering system 120A, an ED apparatus 130A, a flow control system 140A and a series of flow lines that are described in additional detail below. Additional details of BPED 110A are provided in U.S. Pat. No. 11,629,067, entitled “OCEAN ALKALINITY SYSTEM AND METHOD FOR CAPTURING ATMOSPHERIC CARBON DIOXIDE”, which is incorporated herein by reference in its entirety.\|[0050] Referring to the upper portion of FIG. 3, fluid buffering system 120A includes an optional salt buffer tank 121A-1 utilized to receive and store brine stream (salt solution) 111-1, an acid buffer tank 121A-2 utilized to store an acid solution 112A, and a base buffer tank 121A-3 utilized to store a base solution 113A. Each buffer tank 121A-1 to 121A-3 can be implemented using a standard 1000 L IBC caged tote tank, where salt buffer tank 121A-1 includes a plastic containment unit 122A-1 having an inflow port 123A-1 operably coupled to receive brine stream 111-1 and an outflow port 124A-1 operably coupled to salt chamber(s) 131 of ion exchange stack 135, acid buffer tank 121A-2 includes a plastic containment unit 122A-2 having an inflow port 123A-21 operably coupled to receive acid product stream portion 112A-21 and an outflow port 124A-2 operably coupled to acid chamber(s) 132 of ion exchange stack 135, and base buffer tank 121A-3 includes a plastic containment unit 122A-3 having an inflow port 123A-31 operably coupled to receive base product stream portion 113A-21 and an outflow port 124A-3 operably coupled to base chamber(s) 133 of ion exchange stack 135. Portions of freshwater output stream 115 generated by desalination unit 180 (shown in FIG. 1) and/or portions of reduced-salt stream 111A-2 may be directed to buffering system 120A and utilized to dilute and maintain acid solution 111A and base solution 113A at suitable levels within buffer tanks 121A-2 and 121A-3.\|[0051] Electrodialysis apparatus 130A includes ion exchange stack 135 and is otherwise configured and operates as described above with reference to FIG. 1 to electrochemical process NaCl (salt) molecules provided in brine stream 111-1 such that Cl-ions pass from salt chamber 131 though ion exchange membrane 134-1 into acid chamber 132 to enhance (i.e., decrease the pH of) acid solution 112A, and such that Nat ions pass from salt chamber 131 though ion exchange membrane 134-2 into base chamber 133 to enhance (i.e., increase the pH of) base solution 113A. Ion exchange stack 135 can be surrounded by a water-tight containment housing (not shown) to facilitate the flow of salt solution 111A through salt chamber(s) 131, the flow of acid solution 112A through acid chamber(s) 132, and the flow of base solution 113A through base chamber(s) 133. Cathode 138A− and anode 138A+ are disposed at opposite ends of ion exchange stack 135 and generate an electric field through the chambers in response to an applied voltage differential provided by a suitable voltage source VS, thereby electrochemically processing the salt, acid and base streams in the manner described herein.\|[0052] Similar to BPEDs utilized in OAE systems, flow control system 140A includes various control elements (e.g., pumps, valves etc.) that are collectively configured to direct streams of the acid and base solutions from buffer tanks 121A-2 and 121A-3 through corresponding chambers 132 and 133 of electrodialysis apparatus 130A and then back to buffer tanks 121A-2 to 121A-3 by way of associated conduits (flow lines). Specifically, weak acid stream 112A-1 exits acid buffer tank 121A-2 and is directed into acid chamber 132A by way of acid inflow line 1501A-2 and a pump 145A-21, and strong acid stream 112A-2 exits acid chamber 132A by way of acid outflow line 152A-2, with a first portion 112A-21 being returned to acid buffer tank 121A-2 by way of optional three-way valve 146A-2 and acid return line 153A-2, and a second portion 112A-22 of strong acid stream 112A-2 being diverted out of BPED 110A, e.g., for system maintenance purposes or commercial sale. Similarly, weak base stream 113A-1 exits base buffer tank 121A-3 and is directed into base chamber 133A by way of base inflow line 151A-3 and a pump 145A-31, a portion 113A-21 of strong base stream 113A-2 exiting base chamber 133A by way of base outflow line 152A-3 is returned to base buffer tank 121A-3 by way of three-way valve 146A-3 and a base return line 153A-3, and a second portion 113A-22 of strong base stream 113A-2 is diverted out of BPED 110A, e.g., for OAE purposes (e.g., as described below with reference to FIG. 5) or for commercial sale.\|[0053] BPED 110A differs from BPEDs typically utilized in OAE systems in that, unlike the acid and base solutions, flow control system 140A does not circulate all of weak salt solution exiting ion exchange stack 135 back to the acid/base buffer tanks. Instead, flow control system 140A is configured to direct brine stream 111-1 into salt chamber(s) 131 and to direct at least a portion 111A-21 of reduced-salt stream 111A-2 from salt chamber(s) 131 to mixing device 170 (shown in FIG. 1). Specifically, brine stream 111A-1 exits (flows from) salt buffer tank 121A-1 by way of outflow port 124A-1 and is directed into salt chamber 131 by way of salt inflow line 151A-1 and a first pump 145A-11, and reduced-salt stream 111A-2 exits salt chamber 131 by way of salt outflow line 152A-1. A valve 146A-1 is controlled by the system controller to direct a first portion 111A-21 of reduced-salt stream 111A-2 to mixing device 170 by way of an optional and an associated flow line 153A-1. A benefit of this arrangement is that, when ED apparatus 130A is operated such that reduced-salt stream 111A-2 has a salt concentration lower than that of the saltwater feedstock, less saltwater feedstock must be pumped to and processed by the desalination subsystem (not shown in FIG. 2), thereby reducing both operating energy and maintenance costs in at least some cases. Flow control system 140A also includes an optional valve 146A-4 that controllable by the system controller to direct a first portion 115-1 of freshwater stream 115 (received from desalination unit 180, see FIG. 1) for use as freshwater output stream 115-OUT, and directs second portion 115-2 of freshwater stream 115 to buffering system 120A (i.e., into one or both of acid buffer tank 121A-2 and base buffer tank 121A-3 to replenish acid/base product diverted from electrochemical reactor 110A for other purposes). Note that valve 146A-1 is also controllable to selectively direct a second portion 111A-22 of reduced-salt stream 111A-2 to fluid buffering system 120A for similar reasons.\|[0054] FIG. 3 shows a portion of a BPED system 110B including an ED apparatus 130B that includes an ion exchange stack 135B, an input manifold 136B-1, an output manifold 136B-2 and an electrolyte solution circulation system 139B. ED apparatus 130B may provide additional details regarding the multiple acid, salt and base chambers described above with reference to ED apparatus 130A (FIG. 2). That is, in some embodiments ED apparatus 130A (FIG. 3) is configured to include the features and details of ED apparatus 130B.\|[0055] Ion exchange stack 135B includes multiple acid chambers 131B-1 to 131B-N, multiple salt chambers 132B-1 to 132B-N and multiple base chambers 133B-1 to 133B-N disposed in a repeating series of cells that are arranged in series between two end chambers 137B-1 and 137B-2. For example, a first cell in the series may include salt chamber 131B-1 disposed between associated acid chamber 132B-1 and associated base chamber 133B-1, and a last cell in the series may include salt chamber 131B-N disposed between associated acid chamber 132B-N and associated base chamber 133B-N. Each of the acid, salt and base chambers of ion exchange stack 135B may function as described above with reference to acid chamber 132, salt chamber 131 and base chamber 133, respectively, to process a corresponding portion of one of the acid, salt and base solution streams directed through ion exchange stack 134B by way of input manifold 136B-1 and output manifold 136B-2. That is, input manifold 136B-1 may split weak acid stream 112B-1 (which is received from an acid buffer tank (not shown) by way of acid inflow line 151B-2) such that corresponding portions of the acid stream pass through each acid chamber 131B-1 to 131B-N. Similarly, input manifold 136B-1 receives brine stream 111-1 by way of salt inflow line 151B-1 and splits brine stream 111-1 into multiple stream portions that are directed through salt chambers 131B-1 to 131B-N, and receives weak base stream 113B-1 from a base buffer tank (not shown) by way of base inflow line 151B-3 and splits weak base stream 113B-1 into multiple stream portions that are directed through base chambers 133B-1 to 133B-N. End chambers 137B-1 and 137B-2 may function to conduct an electrolyte solution indicated by “ES” for purposes described below.\|[0056] Ion exchange stack 135B may include four types of ion permeable membranes that are respectively disposed between adjacent acid, salt, base and end chambers and facilitate the ion transfer process utilized to strengthen the base stream and the salt stream during operation of BPED 110B (i.e., when ion exchange stack 135B receives an electric field generated applying voltage potentials V+ and V− to anode 138B+ and cathode 138B−, respectively). The four types of membranes are indicated in FIG. 3 using the prefixes “A”, “K”, “B” and “F”, where membranes A1 to An are anion exchange membranes, membranes K1 to Kn are cation exchange membranes, membranes B1 to Bn are bipolar membranes, and membranes F1 and F2 are end membranes having characteristics described below. Electrolyte solution circulation system 139B may include a reservoir 139B-0 and flow lines 139B-1 to 139B-3 that function to circulate an electrolyte solution 114B through end chambers 137B-1 and 137B-2. That is, electrolyte solution 114B can be pumped from reservoir 139B-0 along first flow line 139B-1 to first end chamber 137B-1, from end chamber 137B-1 along second flow line 139B-2 to second end chamber 137B-2, and from second end chamber 137B-2 along third flow line 139B-3 to reservoir 139B-0. During operation the electrolyte solution may give up Na+ ions at one end of ion exchange stack 134B and reabsorbs Nat ions at the opposing end of ion exchange stack 135B. In some embodiments, electrolyte solution 114B is implemented using sodium sulfate or a semi conductive solution such as sodium hydroxide.\|[0057] FIG. 4 shows a modified desalination system 100D including an electrochemical reactor 110D and a desalination subsystem 160D.\|[0058] Referring to the lower portion of FIG. 4, electrochemical reactor 110D generally includes a fluid buffering system 120D, an ED apparatus 130D and a flow control system 140D. Fluid buffering system 120D includes an acid buffer tank (ABT) 121D-2 and a base buffer tank (BBT) 121D-3. Acid buffer tank 121D-2 stores an aqueous acid solution formed by a portion 112D-21 of an acid product stream 112D-2 exiting ED apparatus 130D and a portion 115D-21 of freshwater stream 115D exiting desalination subsystem 160D and supplies a relatively weak acid stream 112D-1 to ED apparatus 130D. Base buffer tank 121D-3 stores an aqueous base solution formed by a portion 113D-21 of a base product stream 113D-2 exiting ED apparatus 130D and a portion 115D-22 of freshwater stream 115D exiting desalination subsystem 160D and supplies a relatively weak base stream 113D-1 to ED apparatus 130D. ED apparatus 130D includes an ion exchange stack 135D disposed between electrodes 138D− and 138D+, an input manifold 136D-1 and an output manifold 136D-2, and is configured to receive and electrochemically process brine stream 111D-1, weak acid stream 112D-1 and weak base stream 113D-1 in the manner described above to generate reduced-salt stream 111D-2, acid product stream 112D-2 and base product stream 113D-2. Flow control system 140D includes pipes, pumps (indicated by circled arrows) and valves that are configured to direct the various solution flows between desalination subsystem 160D and electrochemical reactor 110D, and to selectively divert a portion 113D-22 of base product stream 113D-2 and a portion 112D-22 of acid product stream 112D-2 for one or more non-OAE purposes (e.g., for sale to a third party, or for system maintenance or commercial purposes). Flow control system 140D also includes flow control valves 146D-1 and 146D-4. Flow control valve 146D-1 effectively divides freshwater 115D exiting RO unit 180D into a first freshwater stream portion 115D-1 that is directed out of system 100D as freshwater output stream 115D-OUT and a second freshwater stream portion 115D-2 directed to fluid buffering system 120D. Flow control valve 146D-4 effectively divides reduced-salt stream 111D-2 into a first reduced-salt stream portion 111D-21 directed to desalination subsystem 160D and a second reduced-salt stream portion 111D-22 directed to fluid buffering system 120D. As discussed below, the system controller may utilize sensors and other control data to determine the flow amounts (flow rates) of each stream portion 111D-21, 111D-22, 115D-1 and 115D-2, and to adjust the operating states of flow control valves 146D-1 and 146D-4 by way of appropriate control signals to achieve the determined flow amounts.\|[0059] Referring to the upper portion of FIG. 4, desalination subsystem 160D includes a pretreatment unit 165D, a mixing tank (mixing device) 170D and a reverse osmosis system (desalination unit) 180D.\|[0060] Pretreatment unit 165D includes a solids filtering device 166D and a metals/biological removal device 168D that are connected in series such that raw saltwater feedstock 51 must pass through both series-connected filtering devices before being supplied to mixing tank 170D. Each filtering device 166D and 168D utilizes an associated filter to remove targeted contaminants from raw saltwater feedstock 51 (e.g., filtering system 166D utilizes one or more filters 167D that are optimize to remove solid particles from feedstock 51, and filtering system 168D utilizes one or more filters 169D that are optimized to remove metals and/or biologic materials from partially filtered seawater/brine 51T1 received from the first filtering system 166D). The order and number of filtering devices may be different from that shown in FIG. 4. As indicated by the arrows in the upper right portion of FIG. 4, the filtered contaminants (e.g. removed solids, metals and/or biological materials) are removed from the feedstock flow path using known techniques, and the resulting treated (filtered) feedstock solution 51T2 (i.e., the treated saltwater feedstock solution that has passed through both filters 167D and 169D) forms a treated saltwater feedstock stream 51T2 that is passed downstream to mixing tank 170D.\|[0061] Mixing tank 170D is configured to receive reduced-salt stream portion 111D-21 (i.e., some or all of reduced-salt stream 111D-2 exiting ED apparatus 130D) and treated saltwater feedstock stream 51T2 from pretreatment unit 165D. Mixing tank 170D is also configured such that treated saltwater 51T and reduced-salt stream 111D-2 combine (intermix) within the mixing tank 165D to form saltwater/reduced-salt mixture 51M, which is then passed to RO system 180D. Mixing tank 170D is configured to generate mixture stream 51M by combining all of reduced-salt stream portion 111-21 received from electrochemical reactor 110 with a corresponding portion of treated/untreated saltwater feedstock 51T2, which may be controlled by way of a feedstock flow control device 171D in a manner similar to that described above with reference to FIG. 1.\|[0062] RO system 180D receives mixtures stream 51M from mixing tank 170D and utilizes a semi-permeable membrane 181D that prevents the passage of salt molecules, whereby brine stream 111D-1 is formed on one side of membrane 181D and permeate (freshwater) passes through membrane 181D and exit as freshwater stream 115D. Similar to conventional desalination processes, freshwater stream 115D generated RO unit 180D has a suitably low salt concentration (e.g., ≤500 ppm), and brine stream 111-1 comprises an aqueous solution having salt content greater than 50,000 ppm (5%), whereby at least a portion of freshwater stream 115D is suitable for use as freshwater output stream 115D-OUT (i.e., suitable for human consumption and other freshwater uses).\|[0063] Modified desalination system 100D also includes a system controller (not shown) that controls the various operations performed by electrochemical reactor 110D and desalination subsystem 160D way of operation/control signals in the manner described above. In addition, the system controller controls the operating states of flow control valves 146D-1 and 146D-4 in response to sensor data and/or externally supplied data to optimize system operations for reasons set forth above. In some embodiments, flow control valve 146D-4 may be controlled to stop all flow of reduced-salt solution to mixing device 170D, for example, when insufficient clean energy is available and/or electrochemical reactor 110D is shut down. During such periods system 100D may be operated in a manner similar to that implemented by a conventional desalination system.\|[0064] FIG. 5 depicts a system 100E according to another embodiment. In the depicted embodiment, system 100E includes an OAE subsystem (electrochemical reactor) 110E, a seawater desalination subsystem 160E and an enhanced ocean weathering (EOW) subsystem 200, whereby system 100E is sometimes referred to herein as an integrated desalination/OAE/EOW system. However, in some embodiments EOW subsystem 200 may be omitted, whereby system 100E may be referred to as an integrated desalination/OAE system (i.e., by way of including OAE subsystem 110E and seawater desalination subsystem 160E). In other embodiments, seawater desalination subsystem 160E may be omitted (e.g., seawater 51 is pumped directly to OAE subsystem 110E), whereby system 100E may be referred to as a hybrid CDR system for reasons that will become clear below. Therefore, although system 100E is depicted as an integrated desalination/OAE/EOW system, it is understood that FIG. 5 also shows an integrated desalination/OAE system and a hybrid CDR system.\|[0065] Referring to seawater desalination subsystem 160E (lower portion of FIG. 5), seawater 51 is pumped or otherwise drawn from ocean 50 into a pretreatment unit 165E (e.g., a nanofiltration, ultrafiltration, chemical precipitation or other water purification system) that is configured to treat (i.e., remove contaminants from) seawater 51. Treated seawater 51T is then mixed with reduced-salt stream 111E-22 in mixing device 170E to form a treated seawater/reduced-salt mixture solution 51M, and then mixture solution 51M is processed by a desalination unit 180E (e.g., a membrane-based or thermal desalination system) to generate freshwater 115E and a byproduct brine stream 111E-1, thereby providing freshwater output stream 115E. In one embodiment, pretreatment unit 165E is configured to remove hardness related minerals HRM (along with other contaminants) such that a hardness of seawater 51 is reduced before being supplied to mixing device 170E. In some embodiments, as indicated by the dashed-line arrow, the hardness related minerals HRM are supplied to a post-production unit 150E and returned to ocean 50 with the ocean alkalinity product and/or alkaline slurry (both discussed below).\|[0066] OAE subsystem 110E includes a fluid buffering system 120E, an ED apparatus 130E and a flow control system that are configured and operate in the manner described in at least one of the previously described embodiments. ED apparatus 130E converts salt provided in brine stream 111E-1 into acid molecules (e.g., HCl) disposed in an acid product stream 112E-2 and base molecules (e.g., NaOH) disposed in a base product stream 113E-2. Base buffer tank 120E includes an acid buffer tank (ABT) that receives a (first) portion 112E-21 of acid product stream 112E-2 and supplies a weak acid stream to ED apparatus 130E, a base buffer tank (BBT) that receives a (first) portion 113E-21 of base product stream 113E-2 and supplies a weak base stream to ED apparatus 130E, and an optional salt buffer tank (SBT) that receives brine stream 111E-1 from desalination unit 180E and supplied brine stream 111E-1 to ED apparatus 130E. Although not depicted in FIG. 5 for clarity, portions of reduced salt stream 111E-2 and/or freshwater stream 115E may be directed to acid buffer tank (ABT) and base buffer tank (BBT) for the make-up and dilution purposes discussed above.\|[0067] System 100E also includes a post-production unit 150E that selectively utilizes a portion 113E-22 of base product stream 113E-2 to generate an ocean alkalinity product 113E-OUT and selectively utilizes a portion 112E-22 of the acid product stream 112E-2 to generate an alkaline slurry 246, and then supplies (e.g., pumps) the ocean alkalinity product 113E-OUT and the alkaline slurry 246 to the ocean 50 at a designated outfall location 50-1 for OAE purposes (i.e., such that both the fully dissolved base substance in the ocean alkalinity product and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide CO2 and mitigate ocean acidification). In the exemplary embodiment, a portion of post-production unit 150E that is considered part of OAE subsystem 100E includes an acid product tank 127E-2, a base product tank 127E-3, an alkalinity product (ALK PROD) generator 153E and a base delivery subsystem 159E. Acid product tank 127E-2 receives and stores a portion 112E-22 of acid product stream 112E-2, and base product tank 127E-3 receives and stores a portion 113E-22 of base product stream 113E-2. Alkalinity product generation unit 153E is configured to generate an ocean alkalinity product 113E-OUT using a base product stream portion 113E-31, which is received from base product tank 127E-3, such that ocean alkalinity product 113E-OUT includes base molecules (NaOH) that are fully dissolved in a salt solution and has a pH level that is a predetermined amount higher than a pH level of the ocean's seawater 51 (e.g., in a target pH range between 8.0 and 9). In some embodiments, the ocean alkalinity product 113E-OUT is generated using a dilution apparatus configured to operate in the manner described in co-owned and co-pending U.S. Published Patent Application No. US 2024-0336503 A1, entitled “PRODUCTION EFFICIENCY OPTIMIZATION FOR BIPOLAR ELECTRODIALYSIS DEVICE”, which was published on Oct. 10, 2024, and is incorporated herein by reference in its entirety. Post-production unit 150E also includes an enhanced ocean weathering (EOW) subsystem 200 that is configured to generate an alkaline slurry 246 using an acid product stream portion 112E-31, which is received from acid product tank 127E-2, by combining acid product stream portion 112-31 with a coarsely-ground alkaline aggregate (rock) such that a reaction between the alkaline aggregate and the acid molecule both neutralizes the acid molecules and etches/weakens the alkaline aggregate. Enhanced ocean weathering subsystem 200 is described in additional detail below with reference to FIG. 6. Base delivery subsystem 159E is configured and controlled by system controller 190E to supply (e.g., pump) at least one of ocean alkalinity product 113E-OUT and alkaline slurry 246 to ocean 50 at a designated outfall location 50-1.\|[0068] System controller 190E is programmed and otherwise configured to control operations of OAE subsystem 110E by way of control signals 191E, to control operations of desalination subsystem 160E by way of control signals 192E, and configured to control operations of post-production unit 150E by way of control signals 193E and 194E such that one or both of alkalinity product 113E-OUT and alkaline slurry 246 are selectively supplied to ocean 50 in safe and efficient manner. In one embodiment, system controller 190E monitors sensors and other data sources (e.g., via data 195E) and controls base delivery system 159E by way of control signal 194E such that ocean alkalinity product 113E-OUT and alkaline slurry 246 are only supplied to ocean 50 when data 195E indicates that sea life adjacent to outfall location 50-1 will not be endangered by the release of these OAE substances. In another embodiment, system controller 190E may monitor one or more sites that provide input data 195E including spot pricing for the base product and/or acid product generated by electrochemical reactor 110E. Controller 190E may then utilize this input data to determine whether the base and/or acid products should be utilized for OAE/EOW purposes, or whether they should be sold to a third-party buyer. For example, when sufficient low/zero-carbon electricity is available from a power grid to offset the desalination process carbon footprint and the base product spot price is sufficiently high, then the controller 190E may direct the post-production unit 150E (e.g., by way of control signals 191E) to divert a base product portion 113E-220 (e.g., some or all of the second base stream portion 113E-22) for sale to a third-party buyer (i.e., instead of directing the base product to ocean 50 as part of ocean alkalinity product 113E-OUT), whereby proceeds from the sale serve to reduce total operating costs of system 100E. Similarly, the control algorithm implemented by system controller 190E may monitor input data 195E from one or more sites that provide spot pricing for the acid product (e.g., HCl), and utilizes this data to determine whether it is more cost effective to neutralize the acid product (e.g., by way of EOW subsystem 200), or if selling the acid product may produce a greater value (i.e., if the acid product spot price is sufficiently high), in which case the controller 190E may direct the post-production unit 150E to divert an acid product portion 112E-220 (e.g., some or all of the second acid stream portion 112E-22) for sale to a third-party buyer.\|[0069] FIG. 6 shows EOW subsystem 200 of integrated desalination/OAE/EOW system 100E (see FIG. 5) according to an exemplary embodiment. EOW subsystem 200 includes an accelerated ocean weathering reaction apparatus 210, a dosing apparatus 230, a slurry generator 240 and a neutralization controller 280. Accelerated ocean weathering reaction apparatus 210 includes a reaction tank 211 configured to contain a process fluid 215 including a mixture of alkaline aggregate 95 and acid product portion 112E-31 until the acid molecules are neutralized and alkaline aggregate 95 is etched/weakened. In some embodiments, alkaline aggregate 95 may be transported from a quarry or other source by a material delivery vehicle 92 and processed by an optional pre-crusher/grinder 201 before the pre-crushed/ground alkaline aggregate 95-1 is delivered into reaction tank 211 by way of an inlet pipe 203. Dosing apparatus includes one or more dosing pumps 231 that receive acid product portion 112E-31 from acid product tank 127E-2 and is controlled by neutralization controller 280 to inject acid product doses 112E-4 into reaction tank 211 by way of an injector 235. Neutralization controller 280 controls the delivery/injection of alkaline aggregate and acid product into reaction tank 211 by way of monitoring a process fluid pH measurement data pHPF generated by a first sensor S1 disposed inside reaction tank 211 and acid product pH measurement data pHAP generated by a second sensor S2 disposed upstream from acid dosing pump(s) 231. During operation neutralization controller 280 controls the injection rate of acid product doses 112E-4 into reaction tank 211 such that a pH level of process fluid 215 is optimized such that acid molecules are neutralized and alkaline aggregate 95 is etched/weakened at a maximum rate. Neutralized product (i.e., a combination of neutralized acid solution and weakened/etched alkaline aggregate) is passed from reaction tank 211 to slurry generator 240 by way of an outlet pipe 241. Slurry generator 240 is configured to generate alkaline slurry 246 by processing (e.g., crushing/grinding) the etched/weakened alkaline aggregate of neutralized product 215N into fine particles, and then passes alkaline slurry 246 to base delivery subsystem 159E (see FIG. 5). In some embodiments, the accelerated weathering reaction causes the release of one or more metal elements (e.g., Nickel, Cobalt, Aluminum, Magnesium, Potassium and/or Lithium) from the alkaline aggregate and the slurry generator 240 is configured reclaim (i.e., separate and remove) the released metal elements from alkaline slurry 246 using known techniques, whereby system costs may be further reduced/offset by way of commercial sale of the reclaimed metals. In some embodiments, the operation of EOW subsystem 200 is controlled by system controller 190E by way of control signals 193E passed to neutralization controller 280.\|[0070] Referring again to FIG. 5, by configuring post-production unit 150E to implement both alkaline production generator 153E and EOW subsystem 200, system 100E implements a hybrid carbon dioxide removal (CDR) process and a reduced ocean acidification (ROA) process that combines some portions of each of a conventional electrochemical ocean alkalinity enhancement (EOAE) process and a conventional EOW process to achieve combined beneficial results (i.e., CDR/ROA-EOAE and CDR/ROA-EOW) achieved by both conventional processes, but changes other portions of each conventional processes in a way that reduces total operating costs (i.e., in comparison to separately performing the two conventional processes). For example, in one embodiment the hybrid CDR system implements the conventional EOAE process portions related to electrochemically processing salt to generate a base substance (e.g., NaOH) and an acid substance (e.g., HCl) and supplying the base substance to the ocean by way of an ocean alkalinity product, and the hybrid CDR system also implements the conventional EOW process portion related to mining and transporting alkaline aggregate/rock. The changes to the conventional EOAE and EOW processes occur after the acid byproduct is produced and after the alkaline rock is transported, whereby the conventional disposal of the acid byproduct and conventional crushing/grinding of the alkaline rock are replaced with an advanced weathering operation that includes combining alkaline rock and the acid product/substance generated by ED apparatus 130. In the embodiment described above with reference to FIG. 6, the advanced weathering operation involves mixing the acid product portion 112E-31 and alkaline rock/aggregate (e.g., olivine/basalt or other mafics/ultramafics) to produce alkaline slurry 246 with a pH between two and eight. As discussed above, slurry generation may include pre-grinding/crushing and/or post-reaction processing of the alkaline rock, but these optional processes require substantially less externally supplied energy than that required by the conventional crushing/grinding process and therefore costs less to perform than conventional acid disposal and crushing/grinding. During the advanced weathering operation, the acid substance in the acid byproduct reacts with alkaline substances in the alkaline rock, thereby weakening and/or increasing the surface area of the alkaline rock and neutralizing the acid substance. During the advanced weathering operation valuable and/or toxic metal constituents of the alkaline aggregate (Ni, Co, Al, Mg, K, Li, etc.) may be reclaimed from the slurry using known techniques. The advanced weathering process proceeds until the acid substance (e.g., HCl) supplied in the acid byproduct is neutralized, at which point the final alkaline slurry has a pH higher than ambient ocean pH (>7.5). The final alkaline slurry could then be dispersed into the ocean via fixed point (e.g., by way of base delivery subsystem 159E) or released from a moving vessel.\|[0071] Although the invention is primarily described herein in the context of seawater desalination and seawater-based OAE systems/methods, various novel aspects described herein may be beneficially utilized in other systems/methods without departing from the spirit and scope of the invention. For example, the chemical reactor implemented by the present invention may be utilized to electrochemically process a wide variety of salt types to generate corresponding base and acid substances. It will be clear to those skilled in the art that the inventive features of the present invention are applicable to these other embodiments as well, and that all of which are intended to fall within the scope of the present invention.	(US20250339810)\|RELATED APPLICATIONS/PATENTS\|[0001] This application claims priority from U.S. Provisional Patent Application No. 63/716,029, entitled “Integrated Ocean Alkalinity Enhancement And Seawater Desalination”, filed on Nov. 4, 2024, which is entirely incorporated herein by reference.\|[0002] This application also claims priority from U.S. Provisional Patent Application No. 63/641,910, entitled “Electrochemical Assisted Ocean Weathering”, filed on May 2, 2024, which is entirely incorporated herein by reference.\|(US20250339810)\|FIELD OF THE INVENTION\|[0003] The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|BACKGROUND\|[0004] As humans burn more and more fossil fuels, the resulting increased carbon dioxide (CO2) concentration in Earth's atmosphere causes both climate change and ocean acidification. The increased atmospheric concentrations of CO2 and other greenhouse gases (e.g., methane) produces climate change by trapping heat close to earth's surface, thereby increasing both air and sea temperatures. Because earth's oceans absorb about 25% of atmospheric CO2, and because the absorbed CO2 dissolves to form carbonic acid that remains trapped in the seawater, the increased atmospheric CO2 concentration caused by burning fossil fuels also produces ocean acidification by way of increasing the amount of CO2 gas dissolved in the ocean.\|[0005] Both climate change and ocean acidification pose Climate change in the form significant threats to humans. of increased global average temperatures can produce several dangerous effects such as the loss of polar ice and corresponding increased sea levels, disease, wildfires and stronger storms and hurricanes. Ocean acidification changes the ocean chemistry that most marine organisms rely on. One concern with ocean acidification is that the decreased seawater pH can lead to the decreased survival of shellfish and other aquatic life having calcium carbonate shells, as well as some other physiological challenges for marine organisms.\|[0006] To avoid dangerous climate change, the international Paris Agreement aims to limit the increase in global average temperature to no more than 1.5° C. to 2° C. above the temperatures of the pre-industrial era. Global average temperatures have already increased by between 0.8° C. and 1.2° C. The Intergovernmental Panel on Climate Change (IPCC) estimates that a ‘carbon budget’ of about 500 GtCO2 (billion tons of carbon dioxide), which corresponds to about ten years at current emission rates, provides a 66% chance of limiting climate change to 1.5° C.\|[0007] In addition to cutting CO2 emissions by curtailing the use of fossil fuels, climate models predict that a significant deployment of Negative Emissions Technologies (NETs) will be needed to avoid catastrophic ocean acidification and global warming beyond 1.5° C. (see “Biophysical and economic limits to negative CO2 emissions”, Smith P. et al., Nat. Clim. Chang. 2016; 6:42-50). Current atmospheric CO2 and other greenhouse gas concentrations are already at dangerous levels, so even a drastic reduction in greenhouse gas emissions would merely curtail further increases, not reduce atmospheric greenhouse gas concentrations to safe levels. Moreover, the reduction or elimination of certain greenhouse gas sources (e.g., emissions from long-distance airliners) would be extremely disruptive and/or expensive and are therefore unlikely to occur soon.\|[0008] Therefore, there is a need to supplement emission reductions with the deployment of NETs, which are systems/processes that serve to reduce existing atmospheric greenhouse gas concentrations by, for example, capturing/removing CO2 from the air and sequestering it for at least 1,000 years. The need for NETs may be explained using a bathtub analogy in which atmospheric CO2 is represented by water contained in a bathtub, ongoing CO2 emissions are represented by water flowing into the tub, and NETs are represented by processes that control water outflow through the tub's drain. In this analogy, reduced CO2 emission rates are represented by partially turning off the water inflow tap—the slower inflow rate provides more time before the tub fills, but the tub's water level will continue to rise and eventually overflow. Using this analogy, although reducing CO2 emissions may slow the increase of greenhouse gas in the atmosphere, critical concentration levels will eventually be reached unless NETs are implemented that can offset the reduced CO2 emission level (i.e., remove atmospheric CO2 at the same rate it is being emitted). Moreover, because greenhouse gas concentrations are already at dangerous levels (i.e., the tub is already dangerously full), there is an urgent need for NETs that are capable of significantly reducing atmospheric CO2 faster than it is being emitted to achieve safe atmospheric concentration levels (i.e., outflow from the tub's drain must be greater than the reduced inflow from the tap to reduce the tub's water to a safe level).\|[0009] NETs can be broadly characterized as Direct Air Capture (DAC) approaches and Ocean Capture approaches. DAC approaches utilize natural (e.g., reforestation) and technology-based methods to extract CO2 directly from the atmosphere. Ocean capture approaches utilize various natural and/or technological processes to remove CO2 from the atmosphere and store it in the ocean as bicarbonate, a form of carbon storage that is stable for over 10,000 years.\|[0010] Electrochemical ocean alkalinity enhancement (electrochemical OAE or EOAE) represents an especially promising ocean capture approach that both reduces atmospheric CO2 and mitigates ocean acidification by generating an ocean alkalinity product (i.e., an aqueous alkaline solution containing a fully dissolved base substance) and supplying the ocean alkalinity product to ocean seawater at a designated outfall location. Electrochemical OAE systems typically generate the required base substance using an electrochemical reactor referred to as a bipolar electrodialysis device (BPED), which generally includes an electrodialysis (ED) apparatus and associated flow control devices configured to perform an electrochemical salt-conversion process that converts salt supplied in an aqueous salt feedstock solution (e.g., seawater) into the base substance and an acid substance. The base substance produced by the BPED is then incorporated into the ocean alkalinity (base) product that is then supplied to the ocean. As the base substance diffuses (disperses) into the surrounding seawater it serves to directly reverse ocean acidification (i.e., by utilizing the base substance in the ocean alkalinity product to increase the ocean seawater's alkalinity), and indirectly reduces atmospheric CO2 (i.e., increasing the ocean seawater's alkalinity increases the ocean's ability to absorb/capture atmospheric CO2). Moreover, because the generated base substance is fully dissolved in the ocean alkalinity product, the electrochemical OAE approach avoids problems associated with other OAE approaches (e.g., dissolution kinetics issues that are associated with conventional mineral OAE approaches).\|[0011] Although electrochemical OAE approaches show great potential in mankind's efforts to combat global warming and ocean acidification, their widespread acceptance as a suitable NET may be predicated on the continued development of OAE system features that minimize cost per unit of captured/removed atmospheric CO2 (LCOC). For economic reasons related to carbon offsets and trading, NETs having relatively low LCOC ratings are typically favored over NETs exhibiting relatively high LCOCs. When calculating a NET's LCOC rating, many factors are taken into consideration, including capital costs (e.g., construction and installation expenses), and ongoing operating costs (e. g., land, water, maintenance, and electrical power expenses). In the case of OAE systems, the amount of atmospheric carbon removed from the atmosphere over an ocean depends on the amount of base substance supplied to the ocean (i.e., by way of the ocean alkalinity product), whereby the LCOC of an OAE system is predominantly determined by its levelized cost of producing each unit of base substance. In terms of the capital cost components of LCOC, OAE systems have an advantage over many NETs in that OAE systems are relatively inexpensive to construct and install, have a relatively small footprint and can be controlled using automated operating systems. Moreover, due to the high energy consumption and wear-related part replacement costs associated with performing the electrochemical salt-conversion process (described above), the most significant operating costs associated with an OAE system arise in the operation of the OAE system's BPED. Therefore, developments that reduce BPED operating costs arguably provide the most promising way to reduce OAE system LCOC.\|[0012] The BPEDs currently utilized in OAE systems are referred to herein as 3-chamber BPEDs for brevity. Such 3-chamber BPEDs may be characterized by utilizing an electrodialysis apparatus having an ion exchange (IE) stack configured in a 3-chamber cell arrangement, and by utilizing a flow control system capable of directing three different aqueous solutions (i.e., a salt feedstock solution, an acid solution, and a base solution) through corresponding salt/acid/base chambers of the IE stack. The IE stack includes multiple 3-chamber cells arranged in series between opposing electrodes, where each 3-chamber cell includes salt, acid and base chambers that respectively serve as parallel flow channels for the aqueous salt, acid and base solutions as they pass through the IE stack (i.e., each cell includes a salt chamber that channels a portion of the salt feedstock solution, an acid chamber that channels a portion of the aqueous acid solution, and a salt/base chamber that channels a portion of the base solution). Each cell's salt chamber is disposed between and separated from the cell's acid and salt/base chambers by corresponding ion exchange membranes, which are configured to facilitate the transfer of sodium and chloride ions from the salt chamber into the base and acid chambers during the electrochemical process. That is, during the electrochemical process an electric field applied across the IE stack by the electrodes produces an ionic current in a direction perpendicular to the parallel flow paths, whereby anions in the salt/base/acid streams (e.g., chloride ions (Cl−) and hydroxide ions (OH−)) move toward the positive electrode (anode) and cations in the salt/base/acid streams (e.g., sodium ions (Nat) and protons (H+)) move toward the positive electrode (anode). This ionic current causes dissociated salt molecules (i.e., sodium ions (Na+) and chloride ions (Cl−)) to exit the salt feedstock stream in opposite directions (i.e., such that the chloride ions (Cl−) pass through a first ion exchange filter from the cell's salt chamber into the cell's acid chamber, and the sodium ions (Nat) pass through a second ion exchange filter into the acid chamber). The chloride ions (Cl−) then combine with protons (H+) to form “new” acid (HCl) molecules in the acid solution stream passing through each cell's acid chamber, and the sodium ions (Nat) combine with hydroxide ions (OH−) to form “new” base (NaOH) molecules in the base solution stream passing through each cell's salt/base chamber. As a result of this electrochemical salt-conversion process, the base solution exiting the IE stack, which combines the base solution flows exiting each of the cells, has a significantly higher concentration of base substance (e.g., NaOH molecules) than before entering the IE stack. Similarly, the acid solution exiting each cell has a higher concentration of acid substance (e.g., HCl molecules) than before entering the IE stack. That is, the 3-chamber IE stack arrangement is configured such that three separate streams exit the ED apparatus: a reduced-salt solution stream (i.e., having a lower salt content than the salt feedstock solution fed into the ED apparatus), an acid product (strong acid) stream including the “new” acid molecules, and a base product (strong base) stream including the “new” base molecules.\|[0013] The main operational costs associated with 3-chamber BPEDs include the cost of externally supplied electricity and maintenance (e.g., replacement part and manual labor) associated with the IE stack, flow control system and other BPED subsystems required to perform the electrochemical salt-conversion process. A majority of the externally supplied electricity needed to power a given BPED operations is consumed by the IE stack (i.e., to generate the electric field that produces the ionic current) and varies in accordance with the BPED's IE stack arrangement. That is, larger capacity IE stacks (i.e., those capable of generating larger amounts of base substance per hour) typically require a larger number of series-connected cells. Although the salt/acid/base solutions are conductive, each ion exchange membranes functions like a resistor that impedes the applied electric field. Therefore, larger capacity IE stacks require larger amounts of externally supplied electricity to maintain an electric field at a suitably strong level across a larger number of cells (i.e., across a larger number of ion exchange membranes) than that required by smaller capacity IE stacks. Moreover, a significant amount is needed to power the flow control system (e.g., the various pumps and valves required to maintain the pressures and flow rates of the salt/acid/base solution streams) and other BPED subsystems, such as feedstock pretreatment units that are typically utilized to remove solids and other contaminants (e.g., divalent ions) from the aqueous salt feedstock solution (e.g., seawater) in order to reduce fouling (e.g., mineral scaling) in the IE stack. BPED maintenance costs include the cost of replacing parts that periodically wear out during normal BPED operations, costs associated with service/labor required to replace these parts, and costs associated with maintenance-related down-time (i.e., the periods of OAE system non-operation that are required to perform maintenance operations). Similar to the cost of externally supplied electricity, maintenance costs are typically higher for BPEDs with larger capacity IE stacks than BPEDs with lower capacity IE stacks due to the need to periodically replace a greater number of expensive ion exchange membranes and the higher expense associated with the replacement of flow control system and pretreatment unit components capable of the required higher flow capacities. Because the effectiveness of OAE systems as a NET is strongly dependent on minimizing LCOC (i.e., minimizing the levelized cost of producing base substance), and because the cost of externally supplied electricity and maintenance costs (e.g., the cost of ion exchange filters/membrane replacement) represent two of the most significant expenses associated with an OAE system's production of base substance, there is a strong motivation to optimize OAE system operations in a way that minimizes these two cost components.\|[0014] Enhanced ocean weathering (EOW) represents another promising ocean capture approach that both reduces atmospheric CO2 and mitigates ocean acidification. EOW involves spreading finely ground alkaline aggregate (e.g., silicate rock, such as basalt) onto large ocean surface areas. The widely dispersed alkaline aggregate captures large amounts of dissolved CO2 while in contact with the ocean water. The alkaline aggregate then sinks below the surface, thereby storing the captured CO2 in the ocean and slowing ocean acidification by way of direct interaction between the ocean's seawater and the alkaline material. A major challenge faced by EOW technologies is how to maximize CO2 drawdown for a given amount of finely ground alkaline aggregate. Currently, the best strategies for addressing this challenge at scale involve crushing/grinding the alkaline rock into extremely small particles and then dispersing these particles over large areas of the ocean to maximize the ratio of surface area to dispersed volume. A problem with these EOW strategies is that both the crushing/grinding and dispersing processes require a significant amount of energy. As explained above, the effectiveness of EOW systems as a NET is strongly dependent on minimizing LCOC, and because the cost of externally supplied electricity to crush/grind the alkaline rock represents one of the most significant expenses associated with an EOW system, there is a strong motivation to optimize EOW system operations in a way that minimizes this cost component.\|[0015] Seawater desalination is the process of removing salt and other contaminants from seawater, making it suitable for human consumption, irrigation, or industrial uses. Seawater desalination allows coastal communities to use a broader variety of water sources than conventional techniques, improving the resilience of water-stressed communities. Seawater desalination will become increasingly important as climate change threatens traditional water resources. As sea levels rise, existing freshwater aquifers for coastal communities are at an increasingly high risk of seawater intrusion, thereby making seawater desalination an important potential tool to help these communities adjust to climate change.\|[0016] Seawater desalination systems utilize either thermal technologies or membrane-based technologies. Thermal desalination systems heat seawater so that H2O evaporates into steam, leaving behind salt and other impurities, then condenses the steam back into liquid freshwater that is suitable for human consumption or other freshwater uses. Membrane-based desalination describes a class of technologies in which saline water passes through a semi-permeable material that allows H2O through but holds back dissolved solids like salts. Reverse osmosis is the most common membrane-based desalination technology that reverses the natural osmosis process (i.e., the natural movement of freshwater from an area of low salt concentration to an area of high salt concentration) by utilizing high-energy pumps to pressurize seawater located on a first side of a semi-permeable material such that passes through the membrane to generate freshwater (sometimes referred to as permeate) on the opposing (second) side of the membrane and leaving behind high-salt content brine (i.e., aqueous solution having a significantly higher salt content than that of seawater) on the first side of the membrane. Note that the pressure required to force freshwater through a membrane is directly proportional to the feedstock solution's salt content (i.e., saltier water having a relatively high salt concentration requires more pressure than less salty water), but this pressure is limited by the strength of the membrane (i.e., the membrane will rupture if the pressure is too high). Therefore, the strength of the membrane effectively creates an upper limit on the salinity of water that can be treated at a given flow volume, and a feedstock solution having a salt content much higher than seawater typically cannot be purified using reverse osmosis technologies.\|[0017] Problems associated with all seawater desalination technologies are related to the disposition of brine, high operating costs and carbon footprint. Both thermal and membrane-based desalination technologies generate brine having a higher salt concentration than seawater that is typically disposed of by supplying the brine into the ocean in a manner that both avoids ecological hazards (e.g., harm to sea life) and does not increase the salt content of the seawater feedstock drawn into the desalination plant (i.e., significant resources are required to disperse the brine over a large ocean region and far from the seawater feedstock input pipe). In addition, although the most efficient thermal desalination processes typically use more energy than membrane-based approaches, even reverse-osmosis seawater desalination consume large amounts of electrical energy (e.g., to drive seawater feed pumps and to achieve the pressures necessary to force permeate through semi-permeable membranes). This high energy consumption causes conventional seawater desalination plants to have both high operating costs and a large carbon footprint (i.e., due to the significant greenhouse gas emissions associated with the generation of the required electrical energy).\|[0018] What is needed is a system/method that reduces seawater desalination system operating costs (i.e., external electricity and/or maintenance) and greenhouse gas emissions while avoiding the ecological hazards and other problems associated with brine disposition. What is also needed is a carbon dioxide removal (CDR) system/method that minimizes LCOC by way of significantly reducing the operating costs associated with conventional EOAE systems/methods (i.e., external electricity and/or maintenance costs) and/or EOW systems/methods (i.e., crushing/grinding costs).\|SUMMARY OF INVENTION\|[0019] In an embodiment the present invention is directed to a modified desalination process and associated method that utilizes an electrochemical process to both mitigate the above-mentioned brine disposition problem and address other problems associated with conventional desalination systems/methods. Similar to conventional desalination processes, the modified desalination system/method is configured to convert a saltwater feedstock (e.g., brackish groundwater or seawater having an initial/first salt concentration) into a desired stream of freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a byproduct stream containing brine (i.e., saline solution having a relatively high (second) salt concentration that is higher than the initial salt content of the saltwater feedstock). According to an aspect, the modified electrochemical process is utilized to mitigate the above-mentioned brine disposition problem by effectively removing most of the salt from the brine stream in a way that effectively converts the brine stream into a reduced-salt stream having a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. According to another aspect, at least some of the reduced-salt stream generated by the electrochemical process is mixed/combined with the saltwater feedstock (i.e., such that the saltwater feedstock is effectively diluted by the reduced-salt stream before performing the desalination process), thereby reducing freshwater production costs by reducing the amount of salt that must be filtered/removed from the saltwater feedstock during the desalination process (i.e., in comparison to conventional processes in which only saltwater feedstock is desalinated).\|[0020] In an embodiment a modified desalination (or other) system includes an electrochemical reactor (e.g., a bipolar electrodialysis apparatus (BPED)), a mixing device and a desalination unit that are cooperatively coupled and configured to perform the modified desalination process mentioned above. The desalination unit utilizes known techniques to convert a saltwater feedstock having an initial (first) salt concentration into a freshwater stream and a brine stream having a relatively high (second) salt concentration, and the system is configured to direct (e.g., by way of pipes and pumps) the brine stream from an output terminal of the desalination unit to an input terminal of the electrochemical reactor. The electrochemical reactor is configured to channel three separate solutions: an aqueous salt solution that enters the reactor as the brine stream and exits as the reduced-salt stream, an aqueous acid solution that enters as a weak acid stream and exits as an acid product stream, and an aqueous base solution that enters as a weak base stream and exits as a base product stream. The electrochemical reactor is also configured to generate the reduced-salt stream by electrochemically processing the brine stream such that at least some of the salt molecules (e.g., NaCl) contained in the brine stream are converted into acid molecules (HCl) contained in the acid product stream and base molecules (NaOH) contained in a base product stream. According to another aspect, the electrochemical processing is performed at a rate that converts/removes a sufficient amount salt from the salt/saline solution such that the (third) salt concentration of the reduced-salt stream leaving the electrochemical reactor is lower than the initial (first) salt concentration of saltwater feedstock, thereby significantly reducing eco-safety risks and other brine disposition issues associated with conventional desalination systems/processes. According to another aspect, the system is further configured to direct (e.g., by way of pipes and pumps) at least some of the reduced-salt stream from the electrochemical reactor to an input terminal of the mixing device, which is configured to mix a saltwater feedstock stream (i.e., untreated feedstock or treated feedstock) with the reduced-salt stream received from the electrochemical reactor such that the resulting mixture stream has a (fourth) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock, and the desalination unit is configured to generate the freshwater stream and the brine stream by processing the mixture stream (desalination fluid) exiting the mixing device. Mixing (combining) the saltwater feedstock with the reduced-salt stream provides the system with two cost-saving benefits over conventional desalination systems: first, the energy cost required to produce each unit of freshwater is reduced because the amount of raw seawater or briny groundwater that must be pumped from a saltwater feedstock source to the desalination unit is reduced by an amount equal to that of the reduced-salt stream; and second, the operating/maintenance costs of the system are reduced by reducing the amount of salt that must be filtered or otherwise separated from the desalinated fluid (i.e., the feedstock/reduced-salt mixture) by the desalination unit. Accordingly, by utilizing an electrochemical reactor to remove salt from the brine stream generated by the desalination process, and then utilizing the reduced-salt stream generated by the electrochemical reactor to supplement/dilute the saltwater feedstock directed into the desalination unit, the modified desalination system both mitigates the above-mentioned brine disposition problem and addresses other problems associated with conventional desalination systems.\|[0021] In some embodiments, the system includes an optional pretreatment unit that is operably coupled between a saltwater feedstock source (e.g., ocean or well) and the mixing device, and is configured to remove solids and other contaminants from a stream (portion) of “raw” saltwater feedstock that has been pumped or otherwise delivered from the saltwater feedstock source (e.g., seawater pumped directly from an ocean or briny groundwater pumped from a well), and is further configured to deliver the resulting treated saltwater feedstock to the mixing device by way of the saltwater feedstock stream. In some embodiments the pretreatment unit includes filtering systems or other devices that function to remove solids and at least some contaminants (e.g., biological material and/or divalent ions) from the received raw saltwater feedstock. In an exemplary embodiment, the pretreatment unit includes one or more series connected filtering devices that utilize associated filters to remove contaminants from raw saltwater feedstock (e.g., a first filtering system that utilizes first filter(s) to remove solid particles from seawater, and a second filtering system that utilizes second filter(s) to selectively remove metals and/or biologic materials of value from the partially filtered seawater/brine received from the first filtering system). The filtered contaminants (e.g. removed solids, metals and/or biological materials) are removed from the feedstock flow path using known techniques, and the resulting treated (filtered) feedstock solution (i.e., the treated saltwater feedstock solution that has passed through the filters) forms the saltwater feedstock stream that is passed downstream to the mixing device for mixing with the reduced-salt stream received from the electrochemical reactor). In another exemplary embodiment, the pretreatment unit includes nanofiltration, ultrafiltration, chemical precipitation or other water purification system(s) that is/are configured to remove contaminants and reduce the hardness of the saltwater feedstock by filtering/removing dissolved metal ions and other hardness related minerals (e.g., calcium (Ca2+), magnesium (Mg2+), carbonate (CO3)2−, and iron (Fe2+/Fe3+)), and the system may be configured to return the filtered/removed hardness related minerals to the ocean by way of the ocean alkalinity product. Utilizing the pretreatment unit further reduces operating and maintenance costs by extending the uninterrupted operating period of the desalination unit. Moreover, because the reduced-salt stream is utilized as described above to reduce the required amount of raw saltwater feedstock, the cost of maintaining pretreatment units is lower than that of conventional desalination systems (i.e., reducing the amount of saltwater feedstock passed through the pretreatment unit reduces the rate of filter replacement or other periodic maintenance). In some embodiments a second ion removal process (e.g., filtering similar to that used to remove harness related minerals) is applied to the byproduct brine stream leaving the desalination unit (i.e., before the brine stream is supplied to the electrochemical reactor 110E), thereby further reducing operating costs. In other embodiments, the pretreatment unit may be omitted, for example, in cases where the raw saltwater feedstock is sufficiently free of contaminants when delivered to the desalination system.\|[0022] In some embodiments, the mixing device is configured to generate the mixture stream supplied to the desalination unit at a constant outflow rate by combining all of the reduced-salt stream received from the electrochemical reactor with a corresponding portion of the treated/untreated saltwater feedstock. As mentioned above, the salt content of the mixture stream exiting the mixing device is inversely proportional to the respective inflow rates of the reduced-salt stream and the saltwater feedstock, so minimizing the mixture stream's salt content (and thus minimizing desalination operating/maintenance costs) involves admitting as much of the reduced-salt stream as possible into the mixing device. In cases where the outflow rate of the mixture stream is determined by the combined reduced-salt stream and saltwater feedstock inflow rates, and is maintained constant (e.g., at the maximum processing rate of the desalination unit), the constant mixture stream outflow rate is achieved by admitting the total amount/inflow of the reduced-salt stream delivered to the mixing device and the controlling (i.e., increasing or decreasing) the saltwater feedstock inflow rate such that the combined inflow rates equal the constant mixture stream outflow rate. In some embodiments, a sensor monitors the flow rate of the reduced-salt stream delivered to the mixing device and a feedstock flow control device is utilized to control a (first) inflow rate of the saltwater feedstock stream into the mixing device, where the system controller controls the feedstock flow control device such that the (first) inflow rate is adjusted (increased/decreased) in accordance with changes (decreases/increases) in the (second) inflow rate of the reduced-salt stream into the mixing device. In some embodiments, the mixing device includes a mixing tank that receives the reduced-salt stream exiting the ED apparatus and a treated saltwater feedstock stream exiting a pretreatment unit such that the two streams intermix within the tank to form the mixture stream. In other embodiments, the mixing device may be implemented, for example, using interconnecting pipes or other mixing structures.\|[0023] As set forth above, the desalination unit functions to desalinate the mixture stream received from the mixing device to generate freshwater and the high-salt brine/feedstock stream. In some embodiments, the desalination unit utilizes a known desalination device/process (e.g., thermal desalination or membrane-based desalination) to separate the mixture stream into the desired freshwater (permeate) stream and the byproduct brine stream. In an exemplary embodiment, the desalination unit utilizes a reverse osmosis (RO) system including a semi-permeable membrane that prevents the passage of salt molecules, whereby the brine stream is formed on one side of the membrane and permeate (freshwater) passes to the opposing side of the membrane. Similar to conventional desalination processes, the freshwater generated by the desalination unit has a suitably low salt concentration (e. g., ≤500 ppm), and the brine stream comprises an aqueous solution having salt content greater than 50,000 ppm (5%).\|[0024] In an embodiment the electrochemical reactor is implemented using a bipolar electrodialysis system (BPED) of a type similar to that utilized in existing OAE systems to convert the high-salt brine stream into the reduced-salt stream. The BPED includes an electrodialysis (ED) apparatus that utilizes an ion exchange stack to perform an electrochemical salt-conversion process during which salt supplied in the brine stream is converted into a base substance and an acid substance. In some embodiments, the ion exchange stack comprising a series of salt chambers, acid chambers and base chambers that are arranged in series between opposing electrodes, where each salt chamber is located between and separated from associated pair of adjacent acid and base chambers by an associated intervening ion exchange membrane. The BPED also includes a flow control system including a first portion that is configured to direct the brine stream through the salt chambers of the ion exchange stack, a second portion configured to direct an aqueous acid solution through the acid chambers and a third portion configured to direct an aqueous base solution through the base chambers. During operation the opposing electrodes apply an electric field across the ion exchange stack to electrochemically process salt (e.g., NaCl) in the brine stream disposed in each salt chamber such that chlorine ions (Cl−) pass through first ion exchange membranes and combine with dissociated protons (H+) to form “new” acid molecules (HCl) in the aqueous acid solution disposed in the associated adjacent acid chamber, and such that sodium ions (Na+) pass through second ion exchange membranes and combine with dissociated hydroxide ions (OH−) to form “new” base molecules (NaOH) in the aqueous base solution disposed in the associated adjacent base chamber. In this manner, the electrochemical process causes the acid and base product streams leaving the ED apparatus to have a higher acid and base concentrations, respectively, than the acid/base solutions entering the ED apparatus. Conversely, the electrochemical process causes the reduction (removal) of salt from the brine solution passed through the ED apparatus, whereby the reduced-salt solution stream exiting the ED apparatus has a salt concentration that is substantially lower than that of the brine stream entering the ED apparatus. By utilizing a BPED similar to those used in stand-alone OAE systems (or another electrochemical reactor having a similar salt processing capacity), the reduced-salt solution can be generated with a salt concentration that is equal to or lower than that of seawater (e.g., below 35,000 ppm (3.5%)), thereby addressing the brine disposition issues associated with stand-alone desalination plants.\|[0025] In some embodiments, the electrochemical reactor also includes a fluid buffering system including an acid buffer tank and a base buffer tank that facilitate the circulation of the aqueous acid and base solutions through the ED apparatus. Specifically, the acid buffer tank is configured to contain the aqueous acid solution that is directed (by way of associated flow control elements) into the acid (second) chamber(s) of the ion exchange stack and to receive a first portion of the acid product stream exiting (directed away from) the acid chambers(s). Similarly, the base buffer tank is configured to contain the aqueous base solution that is directed to the base (third) chamber(s) of the ion exchange stack and to receive a first portion of the base product stream exiting the base chamber(s). Note that second portions of the acid and base product streams are typically diverted for other purposes (e. g., maintenance, OAE or commercial sale). As mentioned above, the electrochemical reactor's flow control system is configured such that the brine stream exiting the desalination unit is directed to the ED apparatus, and at least a portion of the reduced-salt stream exiting the ED apparatus is directed to the mixing device. This salt solution flow arrangement differs from BPEDs utilized in conventional OAE systems in which the reduced/depleted salt stream exiting an ED apparatus is typically utilized to replenish (make up) any acid/base product diverted from the electrochemical reactor for other purposes and to control the acid/base concentration (dilution) of the weak acid and base solutions directed to the ED apparatus. To facilitate dilution of the acid and/or solution streams in cases where all of the reduced-salt stream is directed to the mixing device, in one embodiment, the flow control system is further configured to divert some of the freshwater stream exiting the desalination unit such that it flows into the acid buffer tank and/or the base buffer tank. Although utilizing some of the freshwater for acid and/or base dilution reduces the amount of freshwater output from the system, the required dilution amount is typically much less than that produced by the desalination unit, and may provide a net benefit, for example, in cases where high quality acid product is desired (i.e., the acid product's value is typically inversely proportional to the amount of salt in the acid solution). In other embodiments, replenishing for the acid and/or base product streams may be achieved using a portion of the reduced-salt stream or using a mixture of both freshwater and reduced-salt streams.\|[0026] In some embodiments the brine stream exiting the desalination unit may be passed directly to the ED apparatus (i.e., the fluid buffer system may only include an acid buffer tank and a base buffer tank, and omit a salt buffer tank). In other embodiments, the fluid buffer system may include a salt buffer tank that is operably coupled between the desalination unit and the ED apparatus, and serves as a buffer for aqueous salt solution (i.e., such that a portion of the brine stream produced by the desalination unit is stored in the salt buffer tank). In this case, the salt buffer tank may be used to regulate the flow rate of brine into the ED apparatus.\|[0027] In some embodiments, the electrochemical reactor is configured to process brine at a rate that corresponds with a desired maximum freshwater production rate. That is, a desalination unit that is capable of generating freshwater at a relatively high flow rate also generates brine at a relatively high flow rate, so, to avoid the buildup of unprocessed brine, the electrochemical reactor must be capable of converting the brine stream into a corresponding reduced-salt stream at a corresponding flow rate. In addition to suitable flow control and buffer resources, the electrochemical reactor's ED apparatus must be configured to receive and process brine at the corresponding flow rate, for example, by way of providing a sufficient number of cells (i.e., groups of salt, acid and base chambers separated by intervening ion exchange membranes) arranged in series between suitable electrodes, and otherwise configuring the ED apparatus to facilitate the conversion of brine at the relatively high flow rate.\|[0028] In another exemplary embodiment, an integrated (combined) desalination/OAE system includes a seawater desalination subsystem and an OAE subsystem (electrochemical reactor). The seawater desalination subsystem generates a freshwater stream by desalinating seawater pumped or otherwise drawn from a nearby ocean using any of the desalination processes mentioned above. The OAE subsystem includes an ED apparatus that converts salt provided in the byproduct brine stream from the desalination process into acid and base product streams. The system also includes a post-production unit that selectively utilizes a portion of the base product stream to generate an ocean alkalinity product and selectively utilizes a portion of the acid product stream to generate an alkaline slurry, and then supplies (e.g., pumps) the ocean alkalinity product and the alkaline slurry to the ocean at a designated outfall location for OAE and enhanced ocean weathering (EOW) purposes (i.e., such that both the fully dissolved base substance in the ocean alkalinity product and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification). Integrating seawater desalination and at least one of OAE or EOW operations in the manner set forth herein essentially eliminates the ecological concerns associated with conventional stand-alone seawater desalination and significantly decreases total operating costs (i.e., in comparison with conventional stand-alone seawater desalination). That is, because the brine stream has a higher salt concentration than seawater, electrochemically processing the brine stream (i.e., in place of seawater) enhances the generation of ocean alkalinity product by decreasing the amount of externally supplied energy that is required to perform the electrochemical conversion of salt molecules (e.g., NaCl) into acid molecules (e.g., HCl) and base molecules (e.g., NaOH) for a given flow rate through the electrochemical reactor, thereby increasing the base product production efficiency and decreasing total operating cost over conventional stand-alone OAE systems that process seawater, thereby reducing LCOC in comparison to such OAE systems. Moreover, by generating and supplying alkaline ocean product and alkaline slurry to the ocean, the resulting OAE effectively offsets the carbon footprint of the seawater desalination process, and the integrated desalination/OAE system achieves greatly reduces total operating costs over separate (stand-alone) desalination and OAE plants. In addition, utilizing the reduced-salt stream, which is generated as a byproduct of the OAE process, to supplement the seawater (saltwater feedstock) processed by the desalination subsystem reduces operation and maintenance costs over conventional stand-alone seawater desalination plants, for example, by reducing the amount of raw seawater that must be pumped from an ocean and pretreated before desalination. Further, utilizing an electrochemical reactor to process the brine stream that is generated as a byproduct of the desalination process provides additional advantages including: (1) reducing environmental issues and dispersion costs associated with releasing high-salt-content brine directly from the desalination process into an ocean; and (2) reduces maintenance costs by facilitating the use of the generated acid product (e.g., HCl), e.g., to clean semi-permeable and/or ion exchange membranes utilized in the ion exchange stack. Moreover, integrating seawater desalination and OAE subsystems facilitates other benefits such as capital expense reductions achieved by shared plant facilities (e.g., project site and shelter/building), shared saltwater feedstock intake/outfall structures and associated operating costs, shared water treatment operating costs, and shared electrical infrastructure. Further, permitting (government authorization) for desalination plants is difficult in some regions because of eco-safety risks that are primarily due to the increased salinity of the outfall brine—the present invention mitigates this eco-safety risk by utilizing an electrochemical reactor to process the brine such that its final salinity is closer to ambient conditions, thereby leading to an easier permitting process for desalination plants modified in the manner described herein.\|[0029] Although described herein with specific reference to specific modified desalination and integrated desalination/OAE/EOW systems/methods, the present invention may also be utilized to provide other commercially advantageous operations that may achieve at least some of the benefits set forth above. For example, the base product and/or acid product generated by the electrochemical reactor/process may be selectively utilized for non-OAE uses. Although the carbon footprint of the resulting desalination system/process may be higher than that of the combined desalination/OAE approach, the desalination system/process would still have advantages over conventional seawater desalination operations. That is, utilizing the electrochemical reactor to reduce the salt content of the high-salt brine/feedstock stream significantly reduces eco-safety risks and other issues associated with the disposition of the high-salt brine generated by conventional desalination processes. In an exemplary embodiment, the system's controller may monitor one or more sites that provide input data including spot pricing for the base product and/or acid product generated by the electrochemical reactor. The controller may then utilize this input data to determine whether the base and/or acid products should be utilized for OAE/EOW purposes, or whether they should be sold to a third-party buyer. For example, when sufficient low/zero-carbon electricity is available from a power grid to offset the desalination process carbon footprint and the base product spot price is sufficiently high, then the controller may direct the post-production unit to divert the base product (e.g., some or all of the second base stream portion) for sale to a third-party buyer (i.e., instead of directing the base product to the ocean as part of ocean alkalinity product), whereby proceeds from the sale serve to reduce total operating costs of the system. Similarly, the control algorithm implemented by the system's controller may monitor input data from one or more sites that provide spot pricing for the acid product (e.g., HCl) generated by the electrochemical reactor, and utilizes this data to determine whether it is more cost effective to neutralize the acid product (e.g., by way of enhanced ocean weathering), or if selling the acid product may produce a greater value (i.e., if the acid product spot price is sufficiently high), in which case the controller may direct the post-production unit to divert the acid product (e.g., some or all of the second acid stream portion) for sale to a third-party buyer.\|[0030] According to another embodiment, a hybrid carbon dioxide removal (CDR) system includes an electrochemical OAE subsystem configured to generate an ocean alkalinity product, an EOW subsystem configured to generate an alkaline slurry, and a base delivery subsystem configured to supply at least one of the ocean alkalinity product and the alkaline slurry to an ocean to capture/reduce atmospheric carbon dioxide and mitigate ocean acidification. The electrochemical OAE subsystem utilizes an ED device configured to electrochemically process/convert salt into an acid substance and base substance and utilizes an alkaline product generator to generate an ocean alkalinity product including the base substance. In an exemplary embodiment, the EOW subsystem includes an accelerated ocean weathering reaction apparatus and a slurry generator. The accelerated ocean weathering reaction apparatus is configured to combine the acid substance from the electrodialysis device with an alkaline aggregate such that an accelerated ocean weathering reaction between the alkaline aggregate and the acid substance both neutralizes the acid substance and etches/weakens the alkaline aggregate. The slurry generator then receives the neutralized (fully processed) process fluid exiting the reaction apparatus and processes the etched/weakened alkaline aggregate into fine particles, thereby forming the alkaline slurry. In some embodiments, metal elements are released from the alkaline aggregate during the accelerated weathering and slurry generation processes and are reclaimed from the alkaline slurry to offset operating costs. The base delivery subsystem is configured to supply at least one of the ocean alkalinity product and the alkaline slurry to the ocean. By utilizing the acid substance of the electrochemical process to etch/weaken the alkaline aggregate, the accelerated (electrochemically assisted) ocean weathering process implemented by the EOW subsystem produces alkaline slurry at a significantly reduced cost in comparison to conventional EOW systems. That is, the acid substance, which is a byproduct of the electrochemical process and is therefore essentially cost free, serves to etch/weaken the alkaline aggregate, thereby increasing the etched/weakened aggregate's specific surface area and/or facilitating crushing/grinding the etched/weakened aggregate into alkaline particles suitable for ocean dispersal offsetting energy than would be required by conventional EOW crushing/grinding operations. Moreover, during the accelerated weathering operation the alkaline material in the alkaline aggregate neutralizes the acid substance, thereby circumventing acid storage/neutralization issues associated with conventional OAE technologies. Further, by supplying both the electrochemically generated ocean alkalinity product and the alkaline slurry to the ocean, the hybrid CDR system achieves at least the same amount of carbon capture removal and ocean deacidification as that achieved by independently operated conventional OAE and EOW systems using significantly less energy than separate conventional OAE and EOW systems. In some embodiments the CDR system utilizes a desalination subsystem to convert seawater from the ocean into a high-salt-content brine in order to enhance the electrochemical process.\|(US20250339810)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0031] FIG. 1 shows a modified desalination system according to an exemplary embodiment of the present invention;\|[0032] FIG. 2 shows a simplified electrochemical reactor that may be utilized to electrochemically process a brine solution in the modified desalination system of FIG. 1, according to an exemplary specific embodiment;\|[0033] FIG. 3 shows a simplified electrodialysis apparatus that may be utilized by the electrochemical reactor of FIG. 2 to electrochemically convert salt into acid and base products according to another exemplary embodiment;\|[0034] FIG. 4 shows a modified desalination system according to another exemplary embodiment; and\|[0035] FIG. 5 shows an integrated desalination/OAE/EOW system according to another exemplary embodiment of the present invention; and\|[0036] FIG. 6 shows an EOW subsystem of the integrated desalination/OAE/EOW system of FIG. 5 in additional detail according to an exemplary embodiment.\|(US20250339810)\|DETAILED DESCRIPTION\|[0037] The present invention combines desalination and electrochemical systems/processes in a way that converts a saltwater feedstock (e.g., seawater or briny groundwater) into freshwater suitable for human consumption and other freshwater uses, a base substance suitable for OAE purposes, and an acid substance. The invention is primarily described herein with specific reference to a modified desalination system/method that utilizes a desalination subsystem/process to convert saltwater feedstock into freshwater and brine and utilizes an electrochemical reactor/process to convert the brine into a reduced salt solution (i.e., by converting salt in the brine into acid and base substances). In one embodiment, the invention is described with reference to an integrated desalination/OAE/EOW system/method that desalinates seawater to produces freshwater and brine, electrochemically processes the brine to generate acid and base products, utilizes the base product to perform an OAE process, and utilizes the acid product to reduce the energy costs associated with crushing/grinding alkaline aggregate in an EOW process. However, in some embodiments, the systems/methods described herein may be utilized for other purposes, including a stand-alone hybrid HDR system/method or a system/method for generating acid and/or base substances in remote locations. The following description is presented to enable one of ordinary skill in the art to make and use the methods and systems described herein as provided in the context of specific embodiments. Various modifications to the embodiments will be apparent to those with skill in the art, and the general principles defined herein may be applied to other embodiments. Therefore, the methods and systems described herein are not intended to be limited to the particular embodiments shown and described, but are to be accorded the widest scope consistent with the principles and novel features herein disclosed.\|[0038] FIG. 1 depicts a modified desalination system 100 including an electrochemical reactor 110, a desalination subsystem 160 and a system controller 190. Electrochemical reactor 110 performs an electrochemical process in which a high-salt-content brine stream 111-1 is received from the desalination subsystem 160, salt contained in brine stream 111-1 is electrochemically processed (removed), and then at least a portion 111-21 of the resulting reduced-salt stream 111-2 is directed back to desalination subsystem 160. Desalination subsystem 160 performs a modified desalination process in which a mixing device 170 mixes (combines) a saltwater feedstock stream 51T (e.g., seawater or briny groundwater) with reduced-salt stream portion 111-21 received from electrochemical reactor 110 to form a mixture stream 51M, and then a desalination unit 180 processes (desalinates) mixture stream 51M to generate a freshwater stream 115 (i.e., water suitable for human consumption, irrigation, or industrial uses) and brine stream 111-1, which is directed to electrochemical reactor 110. System controller 190 controls the various operations performed by electrochemical reactor 110 and desalination subsystem 160 such that at least a portion of freshwater 115 exiting desalination subsystem 160 is directed out of system 100 as freshwater output stream 115-OUT for fresh water uses. Additional details regarding the various components and processes of system 100 are set forth below.\|[0039] Referring to the left side of FIG. 1, desalination subsystem 160 includes an optional pretreatment unit 165, a mixing device 170 and a desalination unit 180 that process saltwater feedstock 51 to generate freshwater stream 115 and brine stream 111-1.\|[0040] Optional pretreatment unit 165 is configured to treat a “raw” saltwater feedstock stream 51 (i.e., feedstock received directly from an external source, such as raw seawater pumped from an ocean 50, or briny groundwater pumped from a well) by removing (e.g., filtering) solids and other contaminants (e.g., biological material and/or divalent ions) from the raw feedstock. The resulting treated saltwater feedstock exiting pretreatment unit 165 is then supplied to mixing device 170 as saltwater feedstock stream 51T. Note that optional pretreatment unit 165 does not significantly reduce or otherwise change the salt content of the saltwater feedstock (i.e., the treated saltwater forming saltwater feedstock stream 51T has substantially the same initial (first) salt concentration as the raw saltwater forming feedstock stream 51. Pretreatment unit 165 may be omitted, for example, is cases where raw saltwater feedstock stream 51 is sufficiently pure (i.e., free of contaminants), or in embodiments where the raw saltwater feedstock is treated prior to being delivered into desalination subsystem 160. When pretreatment unit 165 is omitted, raw saltwater feedstock is passed directly to mixing device 170 (i.e., saltwater feedstock stream 51T and raw saltwater feedstock stream 51 comprise the same saltwater feedstock stream).\|[0041] Mixing device 170 is configured to receive reduced-salt stream portion 111-21 from electrochemical reactor 110 (i.e., some or all of reduced-salt stream 111-2 exiting ED apparatus 130) and saltwater feedstock stream 51T from pretreatment unit 165. Mixing device 170 utilizes one or more mechanisms (e.g., a mixing tank and/or pumps) to mix (combine) the two streams and to produce a mixture stream 51M including a mixture solution having a (fourth) salt concentration that is between the initial (first) salt concentration of saltwater feedstock stream 51T and an intermediate (third) salt concentration of the reduced-salt stream 111-21. As described in additional detail below, electrochemical reactor 110 is configured to generate reduced-salt stream 111-2 such that the intermediate (third) salt concentration is lower than the initial (first) salt concentration of saltwater feedstock stream 51T. Therefore, mixture stream 51M comprises an aqueous solution having a salt concentration that is lower than the initial salt concentration of the saltwater feedstock. An outlet of mixing device 170 is operably coupled to an inlet of desalination unit 180 such that mixture stream 51M is directed into desalination unit 180. In some embodiments (not shown), the mixing process performed by mixing device 170 may be implemented by either optional pretreatment unit 165 or desalination unit 180.\|[0042] In some embodiments mixing device 170 is configured to generate mixture stream 51M by combining all of reduced-salt stream 111-21 received from electrochemical reactor 110 with a corresponding portion of the treated/untreated saltwater feedstock included in saltwater feedstock stream 51T. That is, the flow rate of mixture stream 51M exiting mixing device 170 is substantially equal to a sum of the inflow rate of reduced-salt stream 111-21 received from electrochemical reactor 110 and the inflow rate of saltwater feedstock stream 51T. In this preferred embodiment, mixture stream 51M includes the total amount of reduced-salt stream 111-21 received from electrochemical reactor 110 and adjusts, if necessary, the inflow rate of saltwater feedstock stream 51T (e.g., by way of a feedstock flow control device 171). For example, assuming desalination unit 180 is configured to process mixture stream 51M at a total flow rate of 100 units per minute, if electrochemical reactor 110 provides reduced-salt stream 111-21 to mixing device 170 at an inflow rate of 30 units/min then the corresponding inflow rate of saltwater feedstock stream 51T is adjusted to equal 70 units/min, and if electrochemical reactor 110 subsequently provides reduced-salt stream 111-21 at an inflow rate of 35 units/min then the corresponding inflow rate of saltwater feedstock stream 51T is adjusted to 65 units/min. Utilizing all of the available reduced-salt stream 111-21 to generate mixture stream 51M minimizes the amount of salt that must be removed from mixture stream 51M by desalination unit 180 (i.e., by minimizing the proportion of saltwater feedstock to reduced-salt solution in mixture stream 51M). Note that variations in the inflow rate of reduced-salt stream 111-21 may occur for purposes of project wide optimization. For example, when acid production is valued higher than freshwater and base production, then freshwater stream portion 115-2 may be directed to acid buffer tank 121-2 (i.e., to increase the value of acid product stream 112-2 by minimizing salt content), whereby more of reduced-salt stream 111-2 may be directed to mixing device 170 as reduced-salt stream portion 111-21. In other cases it may be determined that freshwater and/or base production may be optimized when both freshwater stream portion 115-2 and reduced-salt stream 111-22 are simultaneously directed to acid buffer tank 121-2 and/or base buffer tank 121-3, where the system controller adjusts the fractions of the freshwater and reduced-salt streams to optimize the salt content in the acid and base solutions. In other embodiments, system optimization may be achieved by replenishing (making-up) for the acid product stream 112-22 and/or base product stream 113-22 using only reduced-salt stream portion 111-22 with the remainder of reduced-salt stream 111-2 being directed to mixing device 170 as reduced-salt stream portion 111-21. Whenever system optimization requires a corresponding change (increase/decrease) in the inflow rate of salt stream portion 111-21 to mixing device 170, the system controller makes a corresponding adjustment (decrease/increase) to the inflow rate of saltwater feedstock stream 51T so that the outflow rate of mixture stream 51M remains constant.\|[0043] Desalination unit 180 is configured to perform a desalination process on mixture stream 51M in a manner that generates high-salt brine stream 111-1, which is then directed to electrochemical reactor 130, and freshwater stream 115 comprising water having a salt concentration that is suitable for human consumption (e.g., less than or equal to 0.05% (≤500 ppm). By way of example, when the saltwater feedstock comprises seawater pumped from an ocean, saltwater feedstock stream 51/51T has a salt concentration of about 3.5%, the relatively high salt concentration of brine stream 111-1 may be greater than 5%. As described in additional detail below, in alternative embodiments desalination unit 180 may be implemented using a thermal desalination system, a reverse osmosis system or another membrane-based (or other) desalination system.\|[0044] Referring to the right side of FIG. 1, electrochemical reactor 110 includes a fluid buffering system 120, an electrochemical reactor 130 and a flow control system. As set forth in additional detail below, electrochemical reactor 110 is configured to generate reduced-salt stream 111-2 by electrochemically processing the brine stream 111-1 such that at least some of the salt molecules (e.g., NaCl) contained in brine stream 111-1 are converted into acid molecules (e.g., HCl) contained in an acid product stream 112-2 and base molecules (NaOH) contained in a base product stream 113-2, and such that the reduced-salt stream 111-2 exiting the electrochemical reactor 110 has a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. Note that electrochemical reactor 110 is greatly simplified for descriptive purposes, and that additional details regarding its construction and operation are provided below with reference to the exemplary embodiments depicted in FIGS. 2 to 5.\|[0045] Fluid buffering system 120 includes an acid buffer tank (ABT) 121-2 and a base buffer tank 121-3. Acid buffer tank 121-2 is configured to contain an aqueous acid solution that is circulated through reactor 130 by way of associated flow control structures (e.g., pipes and pumps) such that a relatively weak acid stream 112-1 is directed from acid buffer tank 121-2 to reactor 130 and at least a portion 112-21 of a relatively strong acid product stream 112-2 leaving reactor 130 is directed back to acid buffer tank 121-2. Base buffer tank 121-3 is configured to contain an aqueous base solution that is circulated through reactor 130 by way of associated flow control structures such that a relatively weak base stream 113-1 is directed from base buffer tank 121-3 to reactor 130 and at least a portion 113-21 of a relatively strong base product stream 113-2 leaving reactor 130 is directed back to base buffer tank 121-3. In some embodiments, the flow control system is further configured to direct a portion 115-2 of freshwater 115 into one or more of acid buffer tank 121-2 and base buffer tank 121-3 to dilute the weak solutions directed into reactor 130.\|[0046] ED apparatus 130 generally includes an ion exchange (IE) stack 135 that is disposed between two electrodes (i.e., anode 138+ and cathode 138−). IE stack 135 typically includes multiple cells arranged in series between electrodes 138+ and 138−, where each cell includes three chambers that respectively serve as parallel flow channels for the aqueous salt, acid and base solutions as they pass through IE stack 135. For brevity and clarity, only one cell of IE 135 is depicted in FIG. 1, which is made up of a salt chamber 131 that functions to channel a portion of the aqueous salt solution, an acid chamber 132 that channels a portion of the aqueous acid solution, and a base chamber 133 that channels a portion of the aqueous base solution. Each cell's salt chamber 131 is disposed between and separated from the cell's acid chamber 132 and base chamber 133 by corresponding ion exchange membranes 134-1 and 134-2, which are configured to facilitate the transfer of sodium and chloride ions from the salt chamber into the base and acid chambers during the electrochemical process as described below. ED apparatus 130 also includes manifold or other structures (not shown) that are configured to cooperate with the flow control resources of BPED 110 to direct the three different (i.e., a salt, acid and base) aqueous solutions through corresponding salt/acid/base chambers of IE stack 135. Specifically, the aqueous salt solution enters IE stack 135 as brine stream 111-1 that is divided and directed (e.g., by an input manifold, not shown) into the inlet of each cell's salt flow channel 131, and the aqueous salt solution exits the IE stack 135 by way of an outlet of each cell's salt flow channel 131 (and an outlet manifold, not shown) as reduced-salt stream 111-2. Similarly, the aqueous acid solution enters IE stack 135 as a weak acid stream 112-1 that is directed into the inlet of each cell's acid flow channel 132 and exits the IE stack 135 by way of an outlet of each cell's acid flow channel 132 as acid product stream 112-2. Finally, the aqueous base solution enters IE stack 135 as a weak base stream 113-1 that is directed into the inlet of each cell's base flow channel 133 and exits the IE stack 135 by way of an outlet of each cell's base flow channel 133 as base product stream 113-2.\|[0047] During the electrochemical process the three (salt, acid and base) aqueous solutions are directed through IE stack 135 along parallel flow paths (e.g., in the vertical direction) while a stack voltage VSTACK is applied to electrodes 138+ and 138−. When stack voltage VSTACK is sufficiently strong, the resulting electric field E produces an ionic current across IE stack 135 in a direction perpendicular to the parallel flow paths (e.g., in the horizontal direction). This ionic current causes dissociated salt molecules (i.e., sodium ions (Na+) and chloride ions (Cl−)) to exit brine stream 111-1 in opposite directions (i.e., such that the chloride ions (Cl−) pass through ion exchange filter 138-1 from salt chamber 131 into the acid chamber 132, and the sodium ions (Nat) pass through ion exchange filter 138-2 into base chamber 133). The chloride ions (Cl−) then combine with protons (H+) to form “new” acid molecules (HCl) in the acid solution stream flowing through acid chamber 132, and the sodium ions (Na+) combine with hydroxide ions (OH−) to form “new” base molecules (NaOH) in the base solution stream flowing through base chamber 133. As a result of this electrochemical salt-conversion process, base product stream 113-2 exits each cell's base chamber 133 with a significantly higher concentration of base molecules than weak base stream 113-1 (i.e., the aqueous base solution before it enters IE stack 135). Similarly, acid product stream 112-2 exiting each cell's acid chamber 132 has a higher concentration of acid molecules than that of weak acid stream 112-1. Note that, because salt is converted (consumed) to generate the acid and base molecules, reduced-salt stream 111-2 exiting each cell's salt chamber 131 has a lower salt concentration than inflowing brine stream 111-1.\|[0048] Referring to the lower left portion of FIG. 1, system controller 190 controls the various operations performed by electrochemical reactor 110 by way of operation/control signals 191, and controls the various operations performed by desalination subsystem 160 way of operation/control signals 192 such that at least a portion of the freshwater 115 exiting desalination unit 180 is directed out of system 100 as freshwater output stream 115-OUT. In an embodiment system controller 190 controls the operating state of ED apparatus 130 such that the above-described electrochemical process is performed at a rate that converts/removes a sufficient amount salt from brine stream 111-1 such that reduced-salt stream 111-2 leaving electrochemical reactor 110 has a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. In some embodiments system controller 190 controls a flow rate of mixture stream 51M into desalination unit 180 using sensor data from sensors configured to measure the flow rate of reduced-salt stream portion 111-21 (i.e., some or all of reduced-salt stream 111-2) from electrochemical reactor 110 into mixing device 170 and using a feedstock flow control device (e.g., pump or valve) to control the associated flow rate of saltwater feedstock stream 51T into mixing device 170. Note that, because the salt concentration of reduced-salt stream 111-2 is lower than the initial (first) salt concentration of saltwater feedstock 51/51T, any non-zero flow rate of reduced-salt stream portion 111-21 into mixing device 170 causes the solution forming mixture stream 51M to have a (fourth) salt concentration that is lower than the initial (first) salt concentration of saltwater feedstock 51/51T. Therefore, although operational and maintenance costs associated with desalination subsystem 160 may be reduced by way of directing all (i.e., the totality of) reduced-salt stream 111-2 from ED apparatus 130 to mixing device 170, beneficial reductions in total system operating costs may be achieved when reduced-salt stream portion 111-21 includes less than all of reduced-salt stream 111-2, and the remaining portion is redirected for other purposes (e.g., reduced-salt stream portion 111-22 may be used in place of or in combination with freshwater portion 115-2 to replenish (make-up) the acid and base solutions stored in buffer tanks 121-2 and 121-3). In some embodiments, system controller 190 is implemented using one or more processors configured to implement a software-based control algorithm that utilizes one of a proportional integral derivative, machine learning and/or artificial intelligence to coordinate the desalination and OAE processes (described below). In some embodiments, controller 190 controls the operations performed by electrochemical reactor 110 to perform additional functions described in co-owned U.S. Pat. No. 11,629,067, cited above.\|[0049] FIG. 2 shows a generalized bipolar electrodialysis (BPED) system (electrochemical reactor) 110A of a type similar to that utilized in some Ocean alkalinity enhancement (OAE) systems. BPED 110A generally includes a fluid buffering system 120A, an ED apparatus 130A, a flow control system 140A and a series of flow lines that are described in additional detail below. Additional details of BPED 110A are provided in U.S. Pat. No. 11,629,067, entitled “OCEAN ALKALINITY SYSTEM AND METHOD FOR CAPTURING ATMOSPHERIC CARBON DIOXIDE”, which is incorporated herein by reference in its entirety.\|[0050] Referring to the upper portion of FIG. 3, fluid buffering system 120A includes an optional salt buffer tank 121A-1 utilized to receive and store brine stream (salt solution) 111-1, an acid buffer tank 121A-2 utilized to store an acid solution 112A, and a base buffer tank 121A-3 utilized to store a base solution 113A. Each buffer tank 121A-1 to 121A-3 can be implemented using a standard 1000 L IBC caged tote tank, where salt buffer tank 121A-1 includes a plastic containment unit 122A-1 having an inflow port 123A-1 operably coupled to receive brine stream 111-1 and an outflow port 124A-1 operably coupled to salt chamber(s) 131 of ion exchange stack 135, acid buffer tank 121A-2 includes a plastic containment unit 122A-2 having an inflow port 123A-21 operably coupled to receive acid product stream portion 112A-21 and an outflow port 124A-2 operably coupled to acid chamber(s) 132 of ion exchange stack 135, and base buffer tank 121A-3 includes a plastic containment unit 122A-3 having an inflow port 123A-31 operably coupled to receive base product stream portion 113A-21 and an outflow port 124A-3 operably coupled to base chamber(s) 133 of ion exchange stack 135. Portions of freshwater output stream 115 generated by desalination unit 180 (shown in FIG. 1) and/or portions of reduced-salt stream 111A-2 may be directed to buffering system 120A and utilized to dilute and maintain acid solution 111A and base solution 113A at suitable levels within buffer tanks 121A-2 and 121A-3.\|[0051] Electrodialysis apparatus 130A includes ion exchange stack 135 and is otherwise configured and operates as described above with reference to FIG. 1 to electrochemical process NaCl (salt) molecules provided in brine stream 111-1 such that Cl-ions pass from salt chamber 131 though ion exchange membrane 134-1 into acid chamber 132 to enhance (i.e., decrease the pH of) acid solution 112A, and such that Nat ions pass from salt chamber 131 though ion exchange membrane 134-2 into base chamber 133 to enhance (i.e., increase the pH of) base solution 113A. Ion exchange stack 135 can be surrounded by a water-tight containment housing (not shown) to facilitate the flow of salt solution 111A through salt chamber(s) 131, the flow of acid solution 112A through acid chamber(s) 132, and the flow of base solution 113A through base chamber(s) 133. Cathode 138A− and anode 138A+ are disposed at opposite ends of ion exchange stack 135 and generate an electric field through the chambers in response to an applied voltage differential provided by a suitable voltage source VS, thereby electrochemically processing the salt, acid and base streams in the manner described herein.\|[0052] Similar to BPEDs utilized in OAE systems, flow control system 140A includes various control elements (e.g., pumps, valves etc.) that are collectively configured to direct streams of the acid and base solutions from buffer tanks 121A-2 and 121A-3 through corresponding chambers 132 and 133 of electrodialysis apparatus 130A and then back to buffer tanks 121A-2 to 121A-3 by way of associated conduits (flow lines). Specifically, weak acid stream 112A-1 exits acid buffer tank 121A-2 and is directed into acid chamber 132A by way of acid inflow line 1501A-2 and a pump 145A-21, and strong acid stream 112A-2 exits acid chamber 132A by way of acid outflow line 152A-2, with a first portion 112A-21 being returned to acid buffer tank 121A-2 by way of optional three-way valve 146A-2 and acid return line 153A-2, and a second portion 112A-22 of strong acid stream 112A-2 being diverted out of BPED 110A, e.g., for system maintenance purposes or commercial sale. Similarly, weak base stream 113A-1 exits base buffer tank 121A-3 and is directed into base chamber 133A by way of base inflow line 151A-3 and a pump 145A-31, a portion 113A-21 of strong base stream 113A-2 exiting base chamber 133A by way of base outflow line 152A-3 is returned to base buffer tank 121A-3 by way of three-way valve 146A-3 and a base return line 153A-3, and a second portion 113A-22 of strong base stream 113A-2 is diverted out of BPED 110A, e.g., for OAE purposes (e.g., as described below with reference to FIG. 5) or for commercial sale.\|[0053] BPED 110A differs from BPEDs typically utilized in OAE systems in that, unlike the acid and base solutions, flow control system 140A does not circulate all of weak salt solution exiting ion exchange stack 135 back to the acid/base buffer tanks. Instead, flow control system 140A is configured to direct brine stream 111-1 into salt chamber(s) 131 and to direct at least a portion 111A-21 of reduced-salt stream 111A-2 from salt chamber(s) 131 to mixing device 170 (shown in FIG. 1). Specifically, brine stream 111A-1 exits (flows from) salt buffer tank 121A-1 by way of outflow port 124A-1 and is directed into salt chamber 131 by way of salt inflow line 151A-1 and a first pump 145A-11, and reduced-salt stream 111A-2 exits salt chamber 131 by way of salt outflow line 152A-1. A valve 146A-1 is controlled by the system controller to direct a first portion 111A-21 of reduced-salt stream 111A-2 to mixing device 170 by way of an optional and an associated flow line 153A-1. A benefit of this arrangement is that, when ED apparatus 130A is operated such that reduced-salt stream 111A-2 has a salt concentration lower than that of the saltwater feedstock, less saltwater feedstock must be pumped to and processed by the desalination subsystem (not shown in FIG. 2), thereby reducing both operating energy and maintenance costs in at least some cases. Flow control system 140A also includes an optional valve 146A-4 that controllable by the system controller to direct a first portion 115-1 of freshwater stream 115 (received from desalination unit 180, see FIG. 1) for use as freshwater output stream 115-OUT, and directs second portion 115-2 of freshwater stream 115 to buffering system 120A (i.e., into one or both of acid buffer tank 121A-2 and base buffer tank 121A-3 to replenish acid/base product diverted from electrochemical reactor 110A for other purposes). Note that valve 146A-1 is also controllable to selectively direct a second portion 111A-22 of reduced-salt stream 111A-2 to fluid buffering system 120A for similar reasons.\|[0054] FIG. 3 shows a portion of a BPED system 110B including an ED apparatus 130B that includes an ion exchange stack 135B, an input manifold 136B-1, an output manifold 136B-2 and an electrolyte solution circulation system 139B. ED apparatus 130B may provide additional details regarding the multiple acid, salt and base chambers described above with reference to ED apparatus 130A (FIG. 2). That is, in some embodiments ED apparatus 130A (FIG. 3) is configured to include the features and details of ED apparatus 130B.\|[0055] Ion exchange stack 135B includes multiple acid chambers 131B-1 to 131B-N, multiple salt chambers 132B-1 to 132B-N and multiple base chambers 133B-1 to 133B-N disposed in a repeating series of cells that are arranged in series between two end chambers 137B-1 and 137B-2. For example, a first cell in the series may include salt chamber 131B-1 disposed between associated acid chamber 132B-1 and associated base chamber 133B-1, and a last cell in the series may include salt chamber 131B-N disposed between associated acid chamber 132B-N and associated base chamber 133B-N. Each of the acid, salt and base chambers of ion exchange stack 135B may function as described above with reference to acid chamber 132, salt chamber 131 and base chamber 133, respectively, to process a corresponding portion of one of the acid, salt and base solution streams directed through ion exchange stack 134B by way of input manifold 136B-1 and output manifold 136B-2. That is, input manifold 136B-1 may split weak acid stream 112B-1 (which is received from an acid buffer tank (not shown) by way of acid inflow line 151B-2) such that corresponding portions of the acid stream pass through each acid chamber 131B-1 to 131B-N. Similarly, input manifold 136B-1 receives brine stream 111-1 by way of salt inflow line 151B-1 and splits brine stream 111-1 into multiple stream portions that are directed through salt chambers 131B-1 to 131B-N, and receives weak base stream 113B-1 from a base buffer tank (not shown) by way of base inflow line 151B-3 and splits weak base stream 113B-1 into multiple stream portions that are directed through base chambers 133B-1 to 133B-N. End chambers 137B-1 and 137B-2 may function to conduct an electrolyte solution indicated by “ES” for purposes described below.\|[0056] Ion exchange stack 135B may include four types of ion permeable membranes that are respectively disposed between adjacent acid, salt, base and end chambers and facilitate the ion transfer process utilized to strengthen the base stream and the salt stream during operation of BPED 110B (i.e., when ion exchange stack 135B receives an electric field generated applying voltage potentials V+ and V− to anode 138B+ and cathode 138B−, respectively). The four types of membranes are indicated in FIG. 3 using the prefixes “A”, “K”, “B” and “F”, where membranes A1 to An are anion exchange membranes, membranes K1 to Kn are cation exchange membranes, membranes B1 to Bn are bipolar membranes, and membranes F1 and F2 are end membranes having characteristics described below. Electrolyte solution circulation system 139B may include a reservoir 139B-0 and flow lines 139B-1 to 139B-3 that function to circulate an electrolyte solution 114B through end chambers 137B-1 and 137B-2. That is, electrolyte solution 114B can be pumped from reservoir 139B-0 along first flow line 139B-1 to first end chamber 137B-1, from end chamber 137B-1 along second flow line 139B-2 to second end chamber 137B-2, and from second end chamber 137B-2 along third flow line 139B-3 to reservoir 139B-0. During operation the electrolyte solution may give up Na+ ions at one end of ion exchange stack 134B and reabsorbs Nat ions at the opposing end of ion exchange stack 135B. In some embodiments, electrolyte solution 114B is implemented using sodium sulfate or a semi conductive solution such as sodium hydroxide.\|[0057] FIG. 4 shows a modified desalination system 100D including an electrochemical reactor 110D and a desalination subsystem 160D.\|[0058] Referring to the lower portion of FIG. 4, electrochemical reactor 110D generally includes a fluid buffering system 120D, an ED apparatus 130D and a flow control system 140D. Fluid buffering system 120D includes an acid buffer tank (ABT) 121D-2 and a base buffer tank (BBT) 121D-3. Acid buffer tank 121D-2 stores an aqueous acid solution formed by a portion 112D-21 of an acid product stream 112D-2 exiting ED apparatus 130D and a portion 115D-21 of freshwater stream 115D exiting desalination subsystem 160D and supplies a relatively weak acid stream 112D-1 to ED apparatus 130D. Base buffer tank 121D-3 stores an aqueous base solution formed by a portion 113D-21 of a base product stream 113D-2 exiting ED apparatus 130D and a portion 115D-22 of freshwater stream 115D exiting desalination subsystem 160D and supplies a relatively weak base stream 113D-1 to ED apparatus 130D. ED apparatus 130D includes an ion exchange stack 135D disposed between electrodes 138D− and 138D+, an input manifold 136D-1 and an output manifold 136D-2, and is configured to receive and electrochemically process brine stream 111D-1, weak acid stream 112D-1 and weak base stream 113D-1 in the manner described above to generate reduced-salt stream 111D-2, acid product stream 112D-2 and base product stream 113D-2. Flow control system 140D includes pipes, pumps (indicated by circled arrows) and valves that are configured to direct the various solution flows between desalination subsystem 160D and electrochemical reactor 110D, and to selectively divert a portion 113D-22 of base product stream 113D-2 and a portion 112D-22 of acid product stream 112D-2 for one or more non-OAE purposes (e.g., for sale to a third party, or for system maintenance or commercial purposes). Flow control system 140D also includes flow control valves 146D-1 and 146D-4. Flow control valve 146D-1 effectively divides freshwater 115D exiting RO unit 180D into a first freshwater stream portion 115D-1 that is directed out of system 100D as freshwater output stream 115D-OUT and a second freshwater stream portion 115D-2 directed to fluid buffering system 120D. Flow control valve 146D-4 effectively divides reduced-salt stream 111D-2 into a first reduced-salt stream portion 111D-21 directed to desalination subsystem 160D and a second reduced-salt stream portion 111D-22 directed to fluid buffering system 120D. As discussed below, the system controller may utilize sensors and other control data to determine the flow amounts (flow rates) of each stream portion 111D-21, 111D-22, 115D-1 and 115D-2, and to adjust the operating states of flow control valves 146D-1 and 146D-4 by way of appropriate control signals to achieve the determined flow amounts.\|[0059] Referring to the upper portion of FIG. 4, desalination subsystem 160D includes a pretreatment unit 165D, a mixing tank (mixing device) 170D and a reverse osmosis system (desalination unit) 180D.\|[0060] Pretreatment unit 165D includes a solids filtering device 166D and a metals/biological removal device 168D that are connected in series such that raw saltwater feedstock 51 must pass through both series-connected filtering devices before being supplied to mixing tank 170D. Each filtering device 166D and 168D utilizes an associated filter to remove targeted contaminants from raw saltwater feedstock 51 (e.g., filtering system 166D utilizes one or more filters 167D that are optimize to remove solid particles from feedstock 51, and filtering system 168D utilizes one or more filters 169D that are optimized to remove metals and/or biologic materials from partially filtered seawater/brine 51T1 received from the first filtering system 166D). The order and number of filtering devices may be different from that shown in FIG. 4. As indicated by the arrows in the upper right portion of FIG. 4, the filtered contaminants (e.g. removed solids, metals and/or biological materials) are removed from the feedstock flow path using known techniques, and the resulting treated (filtered) feedstock solution 51T2 (i.e., the treated saltwater feedstock solution that has passed through both filters 167D and 169D) forms a treated saltwater feedstock stream 51T2 that is passed downstream to mixing tank 170D.\|[0061] Mixing tank 170D is configured to receive reduced-salt stream portion 111D-21 (i.e., some or all of reduced-salt stream 111D-2 exiting ED apparatus 130D) and treated saltwater feedstock stream 51T2 from pretreatment unit 165D. Mixing tank 170D is also configured such that treated saltwater 51T and reduced-salt stream 111D-2 combine (intermix) within the mixing tank 165D to form saltwater/reduced-salt mixture 51M, which is then passed to RO system 180D. Mixing tank 170D is configured to generate mixture stream 51M by combining all of reduced-salt stream portion 111-21 received from electrochemical reactor 110 with a corresponding portion of treated/untreated saltwater feedstock 51T2, which may be controlled by way of a feedstock flow control device 171D in a manner similar to that described above with reference to FIG. 1.\|[0062] RO system 180D receives mixtures stream 51M from mixing tank 170D and utilizes a semi-permeable membrane 181D that prevents the passage of salt molecules, whereby brine stream 111D-1 is formed on one side of membrane 181D and permeate (freshwater) passes through membrane 181D and exit as freshwater stream 115D. Similar to conventional desalination processes, freshwater stream 115D generated RO unit 180D has a suitably low salt concentration (e.g., ≤500 ppm), and brine stream 111-1 comprises an aqueous solution having salt content greater than 50,000 ppm (5%), whereby at least a portion of freshwater stream 115D is suitable for use as freshwater output stream 115D-OUT (i.e., suitable for human consumption and other freshwater uses).\|[0063] Modified desalination system 100D also includes a system controller (not shown) that controls the various operations performed by electrochemical reactor 110D and desalination subsystem 160D way of operation/control signals in the manner described above. In addition, the system controller controls the operating states of flow control valves 146D-1 and 146D-4 in response to sensor data and/or externally supplied data to optimize system operations for reasons set forth above. In some embodiments, flow control valve 146D-4 may be controlled to stop all flow of reduced-salt solution to mixing device 170D, for example, when insufficient clean energy is available and/or electrochemical reactor 110D is shut down. During such periods system 100D may be operated in a manner similar to that implemented by a conventional desalination system.\|[0064] FIG. 5 depicts a system 100E according to another embodiment. In the depicted embodiment, system 100E includes an OAE subsystem (electrochemical reactor) 110E, a seawater desalination subsystem 160E and an enhanced ocean weathering (EOW) subsystem 200, whereby system 100E is sometimes referred to herein as an integrated desalination/OAE/EOW system. However, in some embodiments EOW subsystem 200 may be omitted, whereby system 100E may be referred to as an integrated desalination/OAE system (i.e., by way of including OAE subsystem 110E and seawater desalination subsystem 160E). In other embodiments, seawater desalination subsystem 160E may be omitted (e.g., seawater 51 is pumped directly to OAE subsystem 110E), whereby system 100E may be referred to as a hybrid CDR system for reasons that will become clear below. Therefore, although system 100E is depicted as an integrated desalination/OAE/EOW system, it is understood that FIG. 5 also shows an integrated desalination/OAE system and a hybrid CDR system.\|[0065] Referring to seawater desalination subsystem 160E (lower portion of FIG. 5), seawater 51 is pumped or otherwise drawn from ocean 50 into a pretreatment unit 165E (e.g., a nanofiltration, ultrafiltration, chemical precipitation or other water purification system) that is configured to treat (i.e., remove contaminants from) seawater 51. Treated seawater 51T is then mixed with reduced-salt stream 111E-22 in mixing device 170E to form a treated seawater/reduced-salt mixture solution 51M, and then mixture solution 51M is processed by a desalination unit 180E (e.g., a membrane-based or thermal desalination system) to generate freshwater 115E and a byproduct brine stream 111E-1, thereby providing freshwater output stream 115E. In one embodiment, pretreatment unit 165E is configured to remove hardness related minerals HRM (along with other contaminants) such that a hardness of seawater 51 is reduced before being supplied to mixing device 170E. In some embodiments, as indicated by the dashed-line arrow, the hardness related minerals HRM are supplied to a post-production unit 150E and returned to ocean 50 with the ocean alkalinity product and/or alkaline slurry (both discussed below).\|[0066] OAE subsystem 110E includes a fluid buffering system 120E, an ED apparatus 130E and a flow control system that are configured and operate in the manner described in at least one of the previously described embodiments. ED apparatus 130E converts salt provided in brine stream 111E-1 into acid molecules (e.g., HCl) disposed in an acid product stream 112E-2 and base molecules (e.g., NaOH) disposed in a base product stream 113E-2. Base buffer tank 120E includes an acid buffer tank (ABT) that receives a (first) portion 112E-21 of acid product stream 112E-2 and supplies a weak acid stream to ED apparatus 130E, a base buffer tank (BBT) that receives a (first) portion 113E-21 of base product stream 113E-2 and supplies a weak base stream to ED apparatus 130E, and an optional salt buffer tank (SBT) that receives brine stream 111E-1 from desalination unit 180E and supplied brine stream 111E-1 to ED apparatus 130E. Although not depicted in FIG. 5 for clarity, portions of reduced salt stream 111E-2 and/or freshwater stream 115E may be directed to acid buffer tank (ABT) and base buffer tank (BBT) for the make-up and dilution purposes discussed above.\|[0067] System 100E also includes a post-production unit 150E that selectively utilizes a portion 113E-22 of base product stream 113E-2 to generate an ocean alkalinity product 113E-OUT and selectively utilizes a portion 112E-22 of the acid product stream 112E-2 to generate an alkaline slurry 246, and then supplies (e.g., pumps) the ocean alkalinity product 113E-OUT and the alkaline slurry 246 to the ocean 50 at a designated outfall location 50-1 for OAE purposes (i.e., such that both the fully dissolved base substance in the ocean alkalinity product and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide CO2 and mitigate ocean acidification). In the exemplary embodiment, a portion of post-production unit 150E that is considered part of OAE subsystem 100E includes an acid product tank 127E-2, a base product tank 127E-3, an alkalinity product (ALK PROD) generator 153E and a base delivery subsystem 159E. Acid product tank 127E-2 receives and stores a portion 112E-22 of acid product stream 112E-2, and base product tank 127E-3 receives and stores a portion 113E-22 of base product stream 113E-2. Alkalinity product generation unit 153E is configured to generate an ocean alkalinity product 113E-OUT using a base product stream portion 113E-31, which is received from base product tank 127E-3, such that ocean alkalinity product 113E-OUT includes base molecules (NaOH) that are fully dissolved in a salt solution and has a pH level that is a predetermined amount higher than a pH level of the ocean's seawater 51 (e.g., in a target pH range between 8.0 and 9). In some embodiments, the ocean alkalinity product 113E-OUT is generated using a dilution apparatus configured to operate in the manner described in co-owned and co-pending U.S. Published Patent Application No. US 2024-0336503 A1, entitled “PRODUCTION EFFICIENCY OPTIMIZATION FOR BIPOLAR ELECTRODIALYSIS DEVICE”, which was published on Oct. 10, 2024, and is incorporated herein by reference in its entirety. Post-production unit 150E also includes an enhanced ocean weathering (EOW) subsystem 200 that is configured to generate an alkaline slurry 246 using an acid product stream portion 112E-31, which is received from acid product tank 127E-2, by combining acid product stream portion 112-31 with a coarsely-ground alkaline aggregate (rock) such that a reaction between the alkaline aggregate and the acid molecule both neutralizes the acid molecules and etches/weakens the alkaline aggregate. Enhanced ocean weathering subsystem 200 is described in additional detail below with reference to FIG. 6. Base delivery subsystem 159E is configured and controlled by system controller 190E to supply (e.g., pump) at least one of ocean alkalinity product 113E-OUT and alkaline slurry 246 to ocean 50 at a designated outfall location 50-1.\|[0068] System controller 190E is programmed and otherwise configured to control operations of OAE subsystem 110E by way of control signals 191E, to control operations of desalination subsystem 160E by way of control signals 192E, and configured to control operations of post-production unit 150E by way of control signals 193E and 194E such that one or both of alkalinity product 113E-OUT and alkaline slurry 246 are selectively supplied to ocean 50 in safe and efficient manner. In one embodiment, system controller 190E monitors sensors and other data sources (e.g., via data 195E) and controls base delivery system 159E by way of control signal 194E such that ocean alkalinity product 113E-OUT and alkaline slurry 246 are only supplied to ocean 50 when data 195E indicates that sea life adjacent to outfall location 50-1 will not be endangered by the release of these OAE substances. In another embodiment, system controller 190E may monitor one or more sites that provide input data 195E including spot pricing for the base product and/or acid product generated by electrochemical reactor 110E. Controller 190E may then utilize this input data to determine whether the base and/or acid products should be utilized for OAE/EOW purposes, or whether they should be sold to a third-party buyer. For example, when sufficient low/zero-carbon electricity is available from a power grid to offset the desalination process carbon footprint and the base product spot price is sufficiently high, then the controller 190E may direct the post-production unit 150E (e.g., by way of control signals 191E) to divert a base product portion 113E-220 (e.g., some or all of the second base stream portion 113E-22) for sale to a third-party buyer (i.e., instead of directing the base product to ocean 50 as part of ocean alkalinity product 113E-OUT), whereby proceeds from the sale serve to reduce total operating costs of system 100E. Similarly, the control algorithm implemented by system controller 190E may monitor input data 195E from one or more sites that provide spot pricing for the acid product (e.g., HCl), and utilizes this data to determine whether it is more cost effective to neutralize the acid product (e.g., by way of EOW subsystem 200), or if selling the acid product may produce a greater value (i.e., if the acid product spot price is sufficiently high), in which case the controller 190E may direct the post-production unit 150E to divert an acid product portion 112E-220 (e.g., some or all of the second acid stream portion 112E-22) for sale to a third-party buyer.\|[0069] FIG. 6 shows EOW subsystem 200 of integrated desalination/OAE/EOW system 100E (see FIG. 5) according to an exemplary embodiment. EOW subsystem 200 includes an accelerated ocean weathering reaction apparatus 210, a dosing apparatus 230, a slurry generator 240 and a neutralization controller 280. Accelerated ocean weathering reaction apparatus 210 includes a reaction tank 211 configured to contain a process fluid 215 including a mixture of alkaline aggregate 95 and acid product portion 112E-31 until the acid molecules are neutralized and alkaline aggregate 95 is etched/weakened. In some embodiments, alkaline aggregate 95 may be transported from a quarry or other source by a material delivery vehicle 92 and processed by an optional pre-crusher/grinder 201 before the pre-crushed/ground alkaline aggregate 95-1 is delivered into reaction tank 211 by way of an inlet pipe 203. Dosing apparatus includes one or more dosing pumps 231 that receive acid product portion 112E-31 from acid product tank 127E-2 and is controlled by neutralization controller 280 to inject acid product doses 112E-4 into reaction tank 211 by way of an injector 235. Neutralization controller 280 controls the delivery/injection of alkaline aggregate and acid product into reaction tank 211 by way of monitoring a process fluid pH measurement data pHPF generated by a first sensor S1 disposed inside reaction tank 211 and acid product pH measurement data pHAP generated by a second sensor S2 disposed upstream from acid dosing pump(s) 231. During operation neutralization controller 280 controls the injection rate of acid product doses 112E-4 into reaction tank 211 such that a pH level of process fluid 215 is optimized such that acid molecules are neutralized and alkaline aggregate 95 is etched/weakened at a maximum rate. Neutralized product (i.e., a combination of neutralized acid solution and weakened/etched alkaline aggregate) is passed from reaction tank 211 to slurry generator 240 by way of an outlet pipe 241. Slurry generator 240 is configured to generate alkaline slurry 246 by processing (e.g., crushing/grinding) the etched/weakened alkaline aggregate of neutralized product 215N into fine particles, and then passes alkaline slurry 246 to base delivery subsystem 159E (see FIG. 5). In some embodiments, the accelerated weathering reaction causes the release of one or more metal elements (e.g., Nickel, Cobalt, Aluminum, Magnesium, Potassium and/or Lithium) from the alkaline aggregate and the slurry generator 240 is configured reclaim (i.e., separate and remove) the released metal elements from alkaline slurry 246 using known techniques, whereby system costs may be further reduced/offset by way of commercial sale of the reclaimed metals. In some embodiments, the operation of EOW subsystem 200 is controlled by system controller 190E by way of control signals 193E passed to neutralization controller 280.\|[0070] Referring again to FIG. 5, by configuring post-production unit 150E to implement both alkaline production generator 153E and EOW subsystem 200, system 100E implements a hybrid carbon dioxide removal (CDR) process and a reduced ocean acidification (ROA) process that combines some portions of each of a conventional electrochemical ocean alkalinity enhancement (EOAE) process and a conventional EOW process to achieve combined beneficial results (i.e., CDR/ROA-EOAE and CDR/ROA-EOW) achieved by both conventional processes, but changes other portions of each conventional processes in a way that reduces total operating costs (i.e., in comparison to separately performing the two conventional processes). For example, in one embodiment the hybrid CDR system implements the conventional EOAE process portions related to electrochemically processing salt to generate a base substance (e.g., NaOH) and an acid substance (e.g., HCl) and supplying the base substance to the ocean by way of an ocean alkalinity product, and the hybrid CDR system also implements the conventional EOW process portion related to mining and transporting alkaline aggregate/rock. The changes to the conventional EOAE and EOW processes occur after the acid byproduct is produced and after the alkaline rock is transported, whereby the conventional disposal of the acid byproduct and conventional crushing/grinding of the alkaline rock are replaced with an advanced weathering operation that includes combining alkaline rock and the acid product/substance generated by ED apparatus 130. In the embodiment described above with reference to FIG. 6, the advanced weathering operation involves mixing the acid product portion 112E-31 and alkaline rock/aggregate (e.g., olivine/basalt or other mafics/ultramafics) to produce alkaline slurry 246 with a pH between two and eight. As discussed above, slurry generation may include pre-grinding/crushing and/or post-reaction processing of the alkaline rock, but these optional processes require substantially less externally supplied energy than that required by the conventional crushing/grinding process and therefore costs less to perform than conventional acid disposal and crushing/grinding. During the advanced weathering operation, the acid substance in the acid byproduct reacts with alkaline substances in the alkaline rock, thereby weakening and/or increasing the surface area of the alkaline rock and neutralizing the acid substance. During the advanced weathering operation valuable and/or toxic metal constituents of the alkaline aggregate (Ni, Co, Al, Mg, K, Li, etc.) may be reclaimed from the slurry using known techniques. The advanced weathering process proceeds until the acid substance (e.g., HCl) supplied in the acid byproduct is neutralized, at which point the final alkaline slurry has a pH higher than ambient ocean pH (>7.5). The final alkaline slurry could then be dispersed into the ocean via fixed point (e.g., by way of base delivery subsystem 159E) or released from a moving vessel.\|[0071] Although the invention is primarily described herein in the context of seawater desalination and seawater-based OAE systems/methods, various novel aspects described herein may be beneficially utilized in other systems/methods without departing from the spirit and scope of the invention. For example, the chemical reactor implemented by the present invention may be utilized to electrochemically process a wide variety of salt types to generate corresponding base and acid substances. It will be clear to those skilled in the art that the inventive features of the present invention are applicable to these other embodiments as well, and that all of which are intended to fall within the scope of the present invention.	Family Number\|(116490379)\|116490379\|Object of Invention\|(US20250339810 A1)\|The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|(WO2025230667 A1)\|The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|Abstract\|(US20250339810 A1)\|A desalination unit processes saltwater feedstock (e.g., seawater) to generate freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a high-salt brine stream. An optional pretreatment unit removes contaminants from the saltwater feedstock before desalination. An electrochemical reactor converts the brine stream into a reduced-salt stream having a salt content lower than the saltwater feedstock by converting salt molecules contained in the brine stream into acid molecules contained in an acid product stream and base molecules contained in a base product stream. A mixing device combines the reduced-salt stream with the saltwater feedstock before the resulting mixture solution is delivered to the desalination unit for desalination. The base product stream leaving the electrochemical reactor may be used for ocean alkalinity enhancement (OAE), and the acid product stream may be used to reduce energy costs associated with crushing/grinding alkaline rock in an enhanced ocean weathering (EOW) process.\|(WO2025230667 A1)\|A desalination unit processes saltwater feedstock (e.g., seawater) to generate freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a high-salt brine stream. An optional pretreatment unit removes contaminants from the saltwater feedstock before desalination. An electrochemical reactor converts the brine stream into a reduced-salt stream having a salt content lower than the saltwater feedstock by converting salt molecules contained in the brine stream into acid molecules contained in an acid product stream and base molecules contained in a base product stream. A mixing device combines the reduced-salt stream with the saltwater feedstock before the resulting mixture solution is delivered to the desalination unit for desalination. The base product stream leaving the electrochemical reactor may be used for ocean alkalinity enhancement (OAE), and the acid product stream may be used to reduce energy costs associated with crushing/grinding alkaline rock in an enhanced ocean weathering (EOW) process.\|Independent Claims\|(US20250339810 A1)\| (...) A hybrid carbon dioxide removal (CDR) system comprising: (...) a base delivery subsystem configured to supply the ocean alkalinity product and the alkaline slurry to an ocean such that both the fully dissolved base substance and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification.\|(WO2025230667 A1)\|16. A hybrid carbon dioxide removal ( CDR) system comprising : an ocean alkalinity enhancement ( OAE ) subsystem including an electrodialysis device configured (...) alkaline slurry to an ocean such that both the fully dissolved base substance and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidi fication .\|	Chemical engineering\|Environmental technology	B01D-053/14/75\|B01D-053/14/93\|B01D-061/02/5\|B01D-061/04\|B01D-061/42/2\|B01D-061/46\|B01D-061/58\|B01D-2252/1035\|B01D-2257/504\|B01D-2258/06\|B01D-2311/04\|B01D-2311/08\|B01D-2311/12\|B01D-2311/2673\|C02F-001/00/8\|C02F-001/04\|C02F-001/04/8\|C02F-001/20\|C02F-001/44/1\|C02F-001/469/3\|C02F-001/469/5\|C02F-2103/08\|C02F-2201/46115\|C02F-2209/06\|Y02A-020/124		B01D-053/14/75\|B01D-053/14/93\|B01D-061/02/5\|B01D-061/04\|B01D-061/42/2\|B01D-061/46\|B01D-061/58\|B01D-2252/1035\|B01D-2257/504\|B01D-2258/06\|B01D-2311/04\|B01D-2311/08\|B01D-2311/12\|B01D-2311/2673\|C02F-001/00/8\|C02F-001/04\|C02F-001/04/8\|C02F-001/20\|C02F-001/44/1\|C02F-001/469/3\|C02F-001/469/5\|C02F-2103/08\|C02F-2201/46115\|C02F-2209/06\|Y02A-020/124	B01D-053/14\|B01D-061/02\|B01D-061/46\|B01D-061/58\|C02F-001/00\|C02F-001/04\|C02F-001/44\|C02F-001/469\|C02F-103/08	B01D-053/14\|B01D-061/02\|B01D-061/46\|B01D-061/58\|C02F-001/00\|C02F-001/04\|C02F-001/44\|C02F-001/469\|C02F-103/08					US11629067\|US20190270660\|CN108623050B\|US20160002082\|CA2834163\|US9382135\|EP1809408\|EP2070583\|US20240336503\|US11629067	US11629067 104545208 WHO=Examiner SELF=Y CAT=I\|US20190270660 85893353 WHO=Examiner SELF=N CAT=I\|CN108623050B 81572078 WHO=Examiner SELF=N CAT=I\|US20160002082 67332528 WHO=Examiner SELF=N CAT=I\|CA2834163 61327814 WHO=Examiner SELF=N CAT=I\|US9382135 44912531 WHO=Examiner SELF=N CAT=I\|EP1809408 61956018 WHO=Examiner SELF=N CAT=I\|EP2070583 1733629 WHO=Examiner SELF=N CAT=I\|US20240336503 111695438 WHO=Applicant SELF=Y\|US11629067 104545208 WHO=Applicant SELF=Y		US11629067; CA2834163; EP1809408; US20160002082; US9382135; EP2070583; CN108623050B; US20190270660; XP026472485; XP093163063; US11629067; US20240336503\|	\|(WO2025/230667)\|International Search Report [Examiner]\|-HOUSE K Z ET AL: "Electrochemical acceleration of chemical weathering for carbon capture and sequestration", ENERGY PROCEDIA, ELSEVIER, NL, vol. 1, no. 1, 1 February 2009 (2009-02-01), pages 4953 - 4960, XP026472485, ISSN: 1876-6102, [retrieved on 20090201], DOI: 10.1016/J.EGYPRO.2009.02.327\|-KURT ZENZ HOUSE: "Electrochemical Acceleration of Chemical Weathering as an Energetically Feasible Approach to Mitigating Anthropogenic Climate Change", ENVIRONMENTAL SCIENCE & TECHNOLOGY, vol. 41, no. 24, 1 December 2007 (2007-12-01), US, pages 8464 - 8470, XP093163063, ISSN: 0013-936X, DOI: 10.1021/es0701816\|-SMITH P ET AL.: "Biophysical and economic limits to negative CO emissions", NAT. CLIM. CHANG., vol. 6, 2016, pages 42 - 50\|	PENDING	(US20250339810)\|PENDING\|(WO2025/230667)\|PENDING	ALIVE	(US20250339810)\|ALIVE\|(WO2025/230667)\|ALIVE	(US20250339810)\|LEGAL DETAILS FOR US20250339810\|Actual or expected expiration date=2045-03-27\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-03-27\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19092576\|Application date=2025-03-27\|Standardized application number=2025US-19092576\|Event publication date=2025-03-27\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-03-27\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-03-27\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: EBB-009\|Event publication date=2025-03-27\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 22888\|Event publication date=2025-03-27\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2025-03-27\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-03-27\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-03-27\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-04-28\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2025-04-29\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-05-05\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2025-05-23\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-05-23\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-08-29\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2025-11-06\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250339810\|Publication stage code=A1\|Publication date=2025-11-06\|Standardized publication number=US20250339810\|Event publication date=2025-11-06\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|(WO2025/230667)\|LEGAL DETAILS FOR WO2025/230667\|Actual or expected expiration date=2027-11-02\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-04-02\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2025/022798\|Application date=2025-04-02\|Standardized application number=2025WO-US22798\|Event publication date=2025-11-06\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/230667\|Publication stage code=A1\|Publication date=2025-11-06\|Standardized publication number=WO2025230667\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2045-04-02\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP25721408\|Event publication date=2025-12-17\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP	(WO2025/230667)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/230667)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/230667)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/230667)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/230667)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UY, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(US20250339810)\|US\|(WO2025/230667)\|WO; EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcPZ7F88luobU0Gd4JhdgzD3JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023106361&ekey=1902&xpn=US20250339810&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19092576/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=KfuhNexKo8%252BlQJXmNbX5EsRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2025/230667)\|US\|(US20250339810)\|US	(WO2025/230667)\|NAME=EBB CARBON, INC. 111 S. Maple Avenue South San Francisco, California 94080 , COUNTRY=US\|(US20250339810)\|NAME=Ebb Carbon, Inc. , CITY=South San Francisco , STATE=CA , COUNTRY=US , ATYP=US Company	(WO2025/230667)\|US	(WO2025/230667)\|NAME=BEVER, Patrick Bever, Hoffman & Harms, LLP 18486 Spring Valley Drive Grass Valley, California 94945 , POSTCODE=94945 , COUNTRY=US	(US20250339810)\|US; US\|(WO2025/230667)\|US; US	(US20250339810)\|NAME=Loretz Jeremy, CITY=Burlingame, STATE=CA , COUNTRY=US \|NAME=Pelman Todd, CITY=Moss Beach, STATE=CA , COUNTRY=US\|(WO2025/230667)\|NAME=LORETZ, Jeremy 1207 Floribunda Avenue, #2 Burlingame, California 94010, POSTCODE=94010, COUNTRY=US \|NAME=PELMAN, Todd 931 Wave Avenue Moss Beach, California 94038, POSTCODE=94038, COUNTRY=US	(WO2025/230667)\|6\|(US20250339810)\|6	3	2					(US20250339810)\|Number of Claims: NCL=20\|Number of Drawings: NDR=6\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1,8,16\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|\|(WO2025/230667)\|Number of Claims: NCL=20\|Extended kind: EXTK=x\|	(US20250339810)\|Provisional Appl: US63/641,910 FDD=2024-05-02 [2024US-63641910]\|Provisional Appl: US63/716,029 FDD=2024-11-04 [2024US-63716029]	(US20250339810)\|ENGLISH (ENG)	(US20250339810)\|Patent\|(WO2025230667)\|Patent	Titre: (US20250339810)\|Integrated Ocean Alkalinity Enhancement And Seawater Desalination Résumé: (US20250339810)\|A desalination unit processes saltwater feedstock (e.g., seawater) to generate freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a high-salt brine stream. An optional pretreatment unit removes contaminants from the saltwater feedstock before desalination. An electrochemical reactor converts the brine stream into a reduced-salt stream having a salt content lower than the saltwater feedstock by converting salt molecules contained in the brine stream into acid molecules contained in an acid product stream and base molecules contained in a base product stream. A mixing device combines the reduced-salt stream with the saltwater feedstock before the resulting mixture solution is delivered to the desalination unit for desalination. The base product stream leaving the electrochemical reactor may be used for ocean alkalinity enhancement (OAE), and the acid product stream may be used to reduce energy costs associated with crushing/grinding alkaline rock in an enhanced ocean weathering (EOW) process.	32	Abstract	gpt-4o-mini	uncertain	The article discusses ocean alkalinity enhancement and desalination, which may relate to enhanced weathering, but the focus is primarily on desalination and not explicitly on CO₂ capture or mineral carbonation.
34	US63/391,662P\|WOUS2023/070710\|IDP00202501664	WOUS2023/070710\|IDP00202501664\|EP23843926\|TW112127364	ID2025/07231\|EP4558651\|TW202417649\|WO2024/020548\|WO2024/020548	108265090	WO2024/020548 A3 2024-04-11 [WO202420548]\|WO2024/020548 A2 2024-01-25 [WO202420548]\|ID2025/07231 A 2025-06-02 [ID202507231]\|EP4558651 A2 2025-05-28 [EP4558651]\|TW202417649 A 2024-05-01 [TW202417649]	2022-07-22\|2023-07-21	2023-07-21\|2023-07-21\|2023-07-21\|2023-07-21	2025-06-02\|2025-05-28\|2024-05-01\|2024-04-11\|2024-01-25		(EP4558651)\|2043-07-21\|(WO2024/020548)\|2026-01-22\|(ID2025/07231)\|2043-07-21\|(TW202417649)\|2043-07-21	(EP4558651)\|Methods for obtaining carbon neutral or carbon negative metals from plants, and related compositions	(EP4558651)\|Provided are methods of extracting metals from rocks and sequestering carbon dioxide. In some embodiments, provided are methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. Provided are also compositions, including metal compositions produced by the methods herein.	METALPLANT PUBLIC BENEFIT\|METOPRON CHARITY	(EP4558651)\|Metalplant Public Benefit Corporation ([US])\|(WO2024/020548)\|METALPLANT PUBLIC BENEFIT CORPORATION ([US])\|(WO2024/020548)\|METALPLANT PUBLIC BENEFIT CORPORATION ([US])\|(ID2025/07231)\|METALPLANT PUBLIC BENEFIT CORPORATION\|(TW202417649)\|METALPLANT PUBLIC BENEFIT CORPORATION ([US])	MATZNER ERIC JASON\|WASSERSON LAURA R	(EP4558651)\|MATZNER, Eric Jason\|WASSERSON, Laura R.	(EP4558651)\|J A Kemp LLP ([GB])\|Reg. Nb: 101669666\|(WO2024/020548)\|ROBERTS, Emily Jane et al. ([US])\|(ID2025/07231)\|Marolita Setiati\|(TW202417649)\|CHEN, CHANG-WEN\|CHANG, CHE LUN\|LO, WEN-MIAO	(WO2024/020548)\|Accordingly, there exists a need in the art for cost-effective methods to remove carbon dioxide from the atmosphere at a gigatonne scale while minimizing the negative impacts on the environment.\|Phytomining refers to the use of hyperaccumulator plant species to concentrate metals from soils and subsequently processing the hyperaccumulator biomass to generate useful metal products.\|	(WO2024/020548)\|1. A method, comprising: mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium, and at least 0.1% each by weight of one or more metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; subjecting the weatherable rock-enriched soil to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process, wherein the chemical weathering process releases the one or more metals; and growing one or more metal hyperaccumulator plant in the weatherable rock-enriched soil, wherein each of the metal hyperaccumulator plants is a hyperaccumulator of at least one of the one or more metals released from the weatherable rock.\|25. A processed nickel composition comprising substantially pure nickel, and one or more of the following (i)-(v):(i) precipitated gypsum; (ii) one or more low weight carboxylic acids; (iii) one or more Ni-containing compounds selected from the group consisting of NiO, Ni(0H)2, nickel sulfides, nickel hydroxides, nickel oxalate, and nickel sulfate; or (iv) one or more carbonates selected from the group consisting of K2CO3, CaCCh, K2Ca(CO3)2. \|26. A nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following (i)-(v):(i) one or more elements selected from the group consisting of Ca, Fe, K, Mg, P, C, H, N, and O; (ii) one or more carbonates selected from the group consisting of K2CO3, CaCCh, K2Ca(CO3)2; (iii) plant cells; (iv) hydroxyapatite or oxy-hydroxyapatite; or (v) one or more oxides selected from the group consisting of NiO, CaO, MgO, and MgNiO2. \|27. A method for sequestering carbon dioxide, comprising: providing a weatherable rock comprising a metal; subjecting the weatherable rock to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide by converting carbon dioxide to bicarbonate or carbonate; and extracting and processing the released metal to provide a metal-enriched composition.\|	(WO2024/020548)\|Provided are methods of extracting metals from rocks and sequestering carbon dioxide. In some embodiments, provided are methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide.\|	(EP4558651)\|CARBON NEGATIVE METAL(100,1)\|OBTAINING CARBON NEUTRAL(100,1)\|PLANT(100,1)\|\|(WO2024/020548)\|SEQUESTERING CARBON DIOXIDE(100,2)\|CARBON NEGATIVE METAL(100,1)\|OBTAINING CARBON NEUTRAL(100,1)\|PLANT(100,1)\|METAL EXTRACTION(72,2)\|ULTRAMAFIC ROCK(62,1)\|ROCK(45,1)\|CARBON DIOXIDE(41,2)\|\|(WO2024/020548)\|SEQUESTERING CARBON DIOXIDE(100,2)\|CARBON NEGATIVE METAL(100,1)\|OBTAINING CARBON NEUTRAL(100,1)\|PLANT(100,1)\|METAL EXTRACTION(72,2)\|ULTRAMAFIC ROCK(62,1)\|ROCK(45,1)\|CARBON DIOXIDE(41,2)\|	(WO2024/020548)\|CLAIMS \|What is claimed is: \|1. A method, comprising: mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium, and at least 0.1% each by weight of one or more metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; subjecting the weatherable rock-enriched soil to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process, wherein the chemical weathering process releases the one or more metals; and growing one or more metal hyperaccumulator plant in the weatherable rock-enriched soil, wherein each of the metal hyperaccumulator plants is a hyperaccumulator of at least one of the one or more metals released from the weatherable rock.\|2. The method of claim 1, further comprising: harvesting the one or more metal hyperaccumulator plant; and processing the one or more harvested metal hyperaccumulator plant to provide one or more substantially pure metal.\|3. The method of claim 1 or 2, wherein the at least one metal comprises nickel, cobalt, chromium, or a combination thereof.\|4. The method of claim 2 or 3, wherein the processing of the harvested metal hyperaccumulator plants comprises: ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash comprising at least 5% of the one or more metal by weight; and refining the metal-enriched ash composition to provide one or more substantially pure metal.\|5. The method of any one of claims 1 to 4, wherein Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock- enriched soil while the metal hyperaccumulator plant is growing.\|6. The method of any one of claims 1 to 5, wherein at least 10 tonnes of carbon dioxide are sequestered for every tonne of metal that is produced.\|7. The method of any one of claims 1 to 6, wherein the weatherable rock comprises ultramafic or mafic rock containing trace levels of the metal.\|8. The method of any one of claims 1 to 7, wherein the weatherable rock comprises serpentine.\|9. The method of any one of claims 1 to 8, wherein the weatherable rock comprises serpentinite.\|10. The method of any one of claims 1 to 9, further comprising mining the weatherable rock.\|11. The method of any one of claims 1 to 10, further comprising transporting the mined weatherable rock from a mining location to a grinding location.\|12. The method of any one of claims 1 to 11, wherein mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock.\|13. The method of any one of claims 1 to 12, wherein the particulate weatherable rock composition has a particle size between 1 pm and 10 cm.\|14. The method of any one of claims 1 to 13, wherein the weatherable rock-enriched soil comprises between 10% and 100% particulate weatherable rock composition by weight.\|15. The method of any one of claims 1 to 14, wherein the metal hyperaccumulator plant is a plant belonging to the genus Odontarrhena.\|16. The method of any one of claims 1 to 15, wherein the metal hyperaccumulator plant is grown inside of a greenhouse.\|17. The method of any one of claims 1 to 16, wherein growing a metal hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil.\|18. The method of any one of claims 1 to 17, wherein the pH of the weatherable rock- enriched soil is at least 7.\|19. The method of any one of claims 4 to 18, wherein the ashing of the harvested metal hyperaccumulator plant comprises: drying the metal hyperaccumulator plant to provide a dried biomass composition; crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a metal-enriched ash composition.\|20. The method of claim 2, wherein the processing of the harvested metal hyperaccumulator plant comprises: directly leaching the harvested metal hyperaccumulator plant using sulfuric acid to provide an acid leachate; purifying the acid leachate using column chromatography to provide a Ni-enriched acid leachate; and processing the Ni-enhanced acid leachate to provide a substantially pure nickel.\|21. The method of claim 3, wherein the at least one metal is nickel, and wherein refining the metal-enriched ash composition comprises: leaching the metal-enriched ash composition to provide a leachate; recovering nickel from the leachate using solvent extraction or an ion exchange resin to obtain a recovered nickel composition; and purifying the recovered nickel composition using electrowinning to obtain a substantially pure nickel.\|22. The method of claim 3, wherein the at least one metal is nickel, and wherein refining the metal-enriched ash composition comprises: acid leaching the metal-enriched ash composition to provide an acid leachate; neutralizing the acid leachate with Ca(OH)2 to provide a first treated leachate; adding NaF to the neutralized leachate to provide a second treated leachate; adding ammonium sulfate to the second treated leachate to provide a third treated leachate; drying the third treated leachate to provide ammonium Ni sulfate hexahydrate (ANSH); and processing the ANSH to obtain a substantially pure nickel.\|23. The method of any one of claims 1 to 22, further comprising quantifying the amount of carbon dioxide that is released or sequestered in any one of steps of the method.\|24. Nickel metal prepared according to the method of any one of claims 1 to 23.\|25. A processed nickel composition comprising substantially pure nickel, and one or more of the following (i)-(v):\|(i) precipitated gypsum; \|(ii) one or more low weight carboxylic acids; \|(iii) one or more Ni-containing compounds selected from the group consisting of NiO, Ni(0H)2, nickel sulfides, nickel hydroxides, nickel oxalate, and nickel sulfate; or \|(iv) one or more carbonates selected from the group consisting of K2CO3, CaCCh, K2Ca(CO3)2. \|26. A nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following (i)-(v):\|(i) one or more elements selected from the group consisting of Ca, Fe, K, Mg, P, C, H, N, and O; \|(ii) one or more carbonates selected from the group consisting of K2CO3, CaCCh, K2Ca(CO3)2; \|(iii) plant cells; \|(iv) hydroxyapatite or oxy-hydroxyapatite; or \|(v) one or more oxides selected from the group consisting of NiO, CaO, MgO, and MgNiO2. \|27. A method for sequestering carbon dioxide, comprising: providing a weatherable rock comprising a metal; subjecting the weatherable rock to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide by converting carbon dioxide to bicarbonate or carbonate; and extracting and processing the released metal to provide a metal-enriched composition.\|28. The method of claim 27, wherein: the subjecting of the weatherable rock comprises growing a metal hyperaccumulator plant in the weatherable rock; and the extracting and the processing of the released metal comprises growing a metal hyperaccumulator plant in the weatherable rock.	(WO2024/020548)\| METHODS FOR OBTAINING CARBON NEUTRAL OR CARBON NEGATIVE METALS FROM PLANTS, AND RELATED COMPOSITIONS \|CROSS-REFERENCE TO RELATED APPLICATIONS \|[0001] This application claims priority to and benefit of U.S. Provisional Application Serial No. 63/391,662, filed July 22, 2022, which is incorporated by reference in its entirety. \|FIELD \|[0002] The present disclosure relates generally to methods of extracting metals from rocks and sequestering carbon dioxide, and more specifically to methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. \|BACKGROUND \|[0003] Carbon dioxide is the dominant greenhouse gas released by human activities and the major contributor to global warming. Carbon sequestration is the process of capturing and storing atmospheric carbon dioxide. It is the only approach that humans can use to actively reduce the amount of carbon dioxide in the atmosphere. Currently, two main types of carbon sequestration are geologic carbon sequestration and biologic carbon sequestration. Current methods for sequestering carbon dioxide, such as underground sequestration, generally face problems related to economic viability, carbon dioxide leakage, and potential contamination of groundwater. Accordingly, there exists a need in the art for cost-effective methods to remove carbon dioxide from the atmosphere at a gigatonne scale while minimizing the negative impacts on the environment. \|BRIEF SUMMARY \|[0004] In some aspects, provided herein are methods and systems that combine enhanced weathering and phytomining to not only sequester carbon dioxide but also extract metals from surrounding soil. Enhanced weathering, which includes terrestrial enhanced weathering and oceanic enhanced weathering, is weathering accelerated by spreading finely ground silicate rock onto surfaces. This helps to accelerate chemical reactions between rocks, water and air. Phytomining refers to the use of hyperaccumulator plant species to concentrate metals from soils and subsequently processing the hyperaccumulator biomass to generate useful metal products. Hyperaccumulators are rare plants that draw up metal from the soil on which they grow, and accumulate high levels of metals in their biomass.\|[0005] In some embodiments, the metals may comprise nickel, cobalt, chromium or any combination thereof. In some embodiments, the methods and systems provided sequester carbon dioxide through a chemical weathering process that results in the release of Mg2+ ions. In some embodiments, the metals are phytomined from serpentinite. Serpentinite is a rock comprising one or more of the serpentine group minerals. Minerals in this group are rich in magnesium and iron. Serpentinite has been called serpentine or serpentine rock, particularly in older geographical texts and in wider cultural settings. In some embodiments, serpentinite is a rock comprising one or more of the serpentine group minerals. In some embodiments, serpentinite is a rock comprising one or more minerals having the chemical formula D3[Si2Os](OH)4, wherein D is selected from the group consisting of Mg, Fe, Ni, Mn, Al, and Zn. In some embodiments, serpentinite is a rock comprising one or more mineral selected from the group consisting of amesite, antigorite, berthierine, brindleyite, caryopilite, chrysotile, cronstedtite, fraipontite, guidottiite, kellyite, lizardite, nepouite, and pecoraite. \|[0006] In some embodiments, the methods and systems provided utilize plant species that are tolerant to soils having high metal contents. In some embodiments, the plants are tolerant of high pH soils. In some embodiments, the plants are tolerant of low nutrient soils. In some embodiments, the plants are hyperaccumulators of nickel. In some variations, provided is a method comprising transporting weatherable rock from a quarry, using mechanical activation to grind the weatherable rock to particles to increase reactive mineral surface area, dispersing the weatherable rock particles into the soil within a plot of land, planting nickel hyperaccumulating plants onto the plot of land to capture the nickel released from the weatherable rock during chemical weathering. In some embodiments, the presence of the nickel hyperaccumulating plants accelerates the chemical weathering of the weatherable rock. In some embodiments, the nickel hyperaccumulating plants may be harvested and further processed to yield a purified nickel composition. In some embodiments, the weatherable rock is ground to a particle size suitable to optimize both the rate of chemical weathering and the rate of nickel accumulation in the hyperaccumulating plant. In some embodiments, grinding the rock to particles comprises grinding the rock to a size of between about 1 pm and about 10 cm. In some variations of the foregoing, the weatherable rock comprises serpentine. In some variations of the foregoing, the weatherable rock comprises serpentinite. \|[0007] In some embodiments, the nickel may be nickel metal in oxidation state 0, or any suitable nickel salts and nickel complexes, such as Ni2+ salts. In some variations, the nickel is a Ni2+ salt or complex. In some embodiments, the nickel may be in an oxidation state of -1, 0, 1, 2, 3, or 4, or any combination thereof. \|[0008] In some variations, the weatherable rock may be obtained from the tailings, waste, or overburden from traditional nickel mines. In some embodiments, the weatherable rock comprises serpentine. In some embodiments, the nickel hyperaccumulating plants are directly irrigated. In some embodiments, the irrigation is accomplished using a continuous irrigation system. In some embodiments, the irrigation is accomplished using an automated irrigation system. \|[0009] In some variations, the methods and systems employ hyperaccumulator plants that are capable of growing in high and even pure levels of serpentine and that are be able to survive and accelerate the weathering rate of the serpentine minerals, especially when fertilized and irrigated. \|[0010] In one aspect, provided is a method for obtaining nickel metal, comprising mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium, and at least 0.1% by weight of nickel to provide a particulate weatherable rock composition, combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil, harvesting the nickel hyperaccumulator plant, and processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel. \|[0011] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash comprising at least 5% nickel by weight, and refining the nickel-enriched ash composition to provide a substantially pure nickel. \|[0012] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises heat treating the harvested nickel hyperaccumulator plant to provide a nickel- enriched ash comprising at least 5% nickel by weight, and refining the nickel-enriched ash composition to provide a substantially pure nickel. \|[0013] In certain embodiments, Mg2+ is leached from the weatherable rock-enriched soil at a rate faster than the observed rate of stationary ultramafic minerals, or minerals without plants growing in them. In certain embodiments, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the nickel hyperaccumulator plant is growing. \|[0014] In other variations, the method may be employed for obtaining one or more metals, including nickel, cobalt, chromium or any combination thereof. In variations where a plurality of metals are obtained, multiple hyperaccumulator plants suitable for harvesting the metals are employed in the process. For example, in some variations of the methods, a nickel hyperaccumulator plant and a cobalt hyperaccumulator plant are used in the weatherable rock-enriched soil to harvest a combination of nickel and cobalt. \|[0015] In some embodiments, at least 10 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. \|[0016] In some embodiments, the weatherable rock comprises ultramafic rock. In some embodiments, the weatherable rock comprises mafic rock. In some embodiments, the weatherable rock comprises less than about 55% silica by weight. In some embodiments, the weatherable rock comprises less than about 45% silica by weight. In some embodiments, the weatherable rock comprises between about 45% and about 55% silica by weight. In some embodiments the weatherable rock comprises one or more minerals selected from the serpentine group. In some embodiments, the weatherable rock comprises olivine. In some embodiments, the weatherable rock comprises serpentinite. In some embodiments, the weatherable rock comprises gabbro or basalt, or a combination. In some embodiments, the weatherable rock comprises a combination of mafic rocks or minerals. \|[0017] In some embodiments, the method comprises mining the weatherable rock. In some embodiments, the method comprises transporting the mined weatherable rock from a mining location to a grinding location. In some embodiments, the method comprises mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock. \|[0018] In some embodiments, the particulate weatherable rock composition has a particle size between 1 pm and 10 cm. In some embodiments, the weatherable rock-enriched soil comprises between 10% and 100% particulate weatherable rock composition by weight. \|[0019] In some embodiments, the nickel hyperaccumulator plant is a plant belonging to the genus Odontarrhena. In some embodiments, the nickel hyperaccumulator plant is grown inside of a greenhouse. In some embodiments, the nickel hyperaccumulator plant is grown under polyethylene film (e.g., a polytunnel). \|[0020] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil. In some embodiments, the pH of the weatherable rock-enriched soil is at least 7. In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises intermittently irrigating the weatherable rock-enriched soil. \|[0021] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises fertilizing the plant. In some embodiments, nitrogen, phosphorus, and potassium (NPK) fertilizers are used to fertilize the plant. In some embodiments, calcium is added to the soil. In some embodiments, boron is used to stimulate flowering in the plant. In some embodiments, soil analysis is used to determine which nutrients are lacking in the soil. In some such embodiments, fertilizer is used to provide the plant with one or more of the nutrients that are determined as lacking in the soil. In some embodiments, exogenous additives are used to increase the available levels of metals in the soil. In some embodiments the exogenous additive comprises citric acid. In some embodiments, potassium is added to the soil. In some embodiments, sulphur-containing compounds are added to the soil. \|[0022] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprises drying the nickel hyperaccumulator plant to provide a dried biomass composition, crushing the dried biomass composition to provide a crushed biomass composition, and burning the crushed biomass composition to provide a nickel-enriched ash composition. \|[0023] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises directly leaching the harvested nickel hyperaccumulator plant using sulfuric acid to provide an acid leachate; purifying the acid leachate using column chromatography to provide a Ni-enriched acid leachate; and further processing the Ni-enhanced acid leachate to provide a substantially pure nickel. \|[0024] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises leaching the nickel-enriched ash composition to provide a leachate; recovering nickel from the leachate using solvent extraction or an ion exchange resin to obtain a recovered nickel composition; and purifying the recovered nickel composition using electrowinning to obtain a substantially pure nickel. \|[0025] It should be understood that, in other variations, the embodiments of the method described above for harvesting nickel may be modified to harvest one or more other metals, such as cobalt and chromium, or any combinations of such metals. \|[0026] In some embodiments, refining the nickel-enriched ash composition comprises: acid leaching the nickel-enriched ash composition to provide an acid leachate; neutralizing the acid leachate with Ca(OH)2 to provide a first treated leachate; adding NaF to the neutralized leachate to provide a second treated leachate; adding ammonium sulfate to the second treated leachate to provide a third treated leachate; drying the third treated leachate to provide ammonium Ni sulfate hexahydrate (ANSH); and processing the ANSH to obtain a substantially pure nickel. \|[0027] In some embodiments, the method further comprises quantifying the amount of carbon dioxide that is released or sequestered in one or more steps of the method. \|[0028] In another aspect, provided is nickel metal prepared according to any of the foregoing methods. \|[0029] In another aspect, provided is a processed nickel composition comprising substantially pure nickel, and one or more of the following: (i) precipitated gypsum, (ii) one or more low weight carboxylic acids, (iii) one or more Ni-containing compounds selected from the group consisting of NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, nickel oxalate, and nickel sulfate, or (v) one or more carbonates selected from the group consisting of K2CO3, CaCO3, K2Ca(CO3)2. \|[0030] In another aspect, provided is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: (i) one or more elements selected from the group consisting of Ca, Fe, K, Mg, P, C, H, N, and O, (ii) one or more carbonates selected from the group consisting of K2CO3, CaCO3, K2Ca(CO3)2, (iii) plant cells, (iv) hydroxyapatite or oxyhydroxyapatite, or (v) one or more oxides selected from the group consisting of NiO, CaO, MgO, and MgNiO2.\|[0031] In yet other aspects, provided is a metal-enriched ash obtained by any of the methods described herein. In some variations, the metal is nickel, cobalt, or chromium, or a combination thereof. \|DESCRIPTION OF THE FIGURES \|[0032] The present application can be understood by reference to the following description taken in conjunction with the accompanying figures. \|[0033] FIG. 1 depicts an exemplary process for obtaining metal using weatherable rock and phytomining. \|[0034] FIG. 2 depicts the different growing conditions employed in the assessment of weathering rates for different soil and plant configurations. \|[0035] FIG. 3 depicts the total amount of magnesium leached under each of the conditions of FIG. 2 over the course of 4 months. \|[0036] FIGS. 4 depicts a diagram of an exemplary field- scale randomized complete block design used to investigate the synergistic combination of nickel phytomining and enhanced weathering. \|[0037] FIG. 5 depicts the pH analysis of topsoils for five application rates approximately eight months after crushed serpentinite rock was applied. \|[0038] FIG. 6 depicts the electrical conductivity analysis of topsoils for five application rates approximately eight months after crushed serpentinite rock was applied. \|[0039] FIG. 7 depicts the amount of nickel in the shoot tissues of hyperaccumulator plants grown on soils treated with eight different application rates of serpentinite rock. \|[0040] FIG. 8 depicts the results from a time-series analysis of topsoil Ni concentrations for five application rates using a Mehlich 1 reagent. \|[0041] FIGS. 9 and 10 depicts the results of statistical analysis of the pH of the soil with respect to application rate and sampling time, respectively. \|[0042] FIGS. 11 and 12 depicts the results of statistical analysis of the electrical conductivity of the soil with respect to application rate and sampling time, respectively.\|[0043] FIGS. 13 and 14 depicts the results of statistical analysis of the ammonium acetate extractable nickel content of the soil with respect to application rate and sampling time, respectively. \|[0044] FIG. 15 depicts the results of statistical analysis of the ammonium acetate extractable magnesium content of the with respect to application rate and sampling time. \|[0045] FIG. 16 depicts a multivariate correlation of the statistical analysis of the soil data. \|[0046] FIG. 17 depicts a diagram of another exemplary field-scale randomized complete block design used to investigate the synergistic combination of nickel phytomining and enhanced weathering. \|[0047] FIG. 18 depicts the life cycle assessment model for an exemplary 1 kilotonne-scale production. \|[0048] FIGS. 19A and 19B depict the life cycle assessment model for an exemplary 1 megatonne-scale production. \|[0049] FIG. 20 depicts additional data used in the life cycle assessment of an exemplary process. \|DETAILED DESCRIPTION \|[0050] The following description sets forth exemplary compositions, methods, systems, parameters and the like. It should be recognized, however, that such description is not intended as a limitation on the scope of the present disclosure but is instead provided as a description of exemplary embodiments. \|[0051] In one aspect, provided herein is a method of sequestering carbon dioxide comprising providing a weatherable rock comprising one or more metals, subjecting the weatherable rock to conditions sufficient to cause the rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the one or more metals, and wherein the alkalinity facilitates the sequestration of carbon dioxide through the conversion of carbon dioxide to bicarbonate or carbonate, and extracting and processing the released metals to provide a metal-enriched composition. In some embodiments, the conditions cited above comprise growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock. In some embodiments, the conditions comprise growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock and continuously irrigating the one or more metal hyperaccumulator plants using a drip irrigation system. In some embodiments, the extracting and processing the released one or more metals comprises growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock, wherein the one or more metal hyperaccumulator plants accumulate the released one or more metals. In some embodiments the extracting and processing the released one or more metals further comprises processing the metal hyperaccumulator biomass using any suitable technique known in the art to prepare a metal-enriched composition. In some embodiments, the one or more metals comprise a heavy metal. In some embodiments, the one or more metals comprise a toxic metal. In some embodiments, the one or more metals comprise a metal selected from the group consisting of Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the one or more metals comprise cobalt. In some embodiments, the one or more metals comprise chromium. In some embodiments, the one or more metals comprise nickel. In some embodiment the one or more metals comprise any metal that can be hyperaccumulated by a hyperaccumulator plant. In some embodiments, providing the weatherable rock comprises mining the weatherable rock. In some embodiments, providing the weatherable rock further comprises mechanically processing the weatherable rock to reduce the particle size of the weatherable rock to between about 1 pm and about 10 cm. In some embodiments, providing the weatherable rock further comprises admixing the weatherable rock with one or more additional growing media including, for example, soil. \|[0052] In one aspect, provided herein is a method of sequestering carbon dioxide comprising providing a weatherable rock comprising a metal, subjecting the weatherable rock to conditions sufficient to cause the rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide through the conversion of carbon dioxide to bicarbonate or carbonate, and extracting and processing the released metal to provide a metal-enriched composition. In some embodiments, the conditions cited above comprise growing a metal hyperaccumulator plant in a medium comprising the weatherable rock. In some embodiments, the conditions comprise growing a metal hyperaccumulator plant in a medium comprising the weatherable rock and continuously irrigating the metal hyperaccumulator plant using a drip irrigation system. In some embodiments, the extracting and processing the released metal comprises growing a metal hyperaccumulator plant in a medium comprising the weatherable rock, wherein the metal hyperaccumulator plant accumulates the released metal. In some embodiments the extracting and processing the released metal further comprises processing the metal hyperaccumulator biomass using any suitable technique known in the art to prepare a metal-enriched composition. In some embodiments, the metal is a heavy metal. In some embodiments, the metal is a toxic metal. In some embodiments, the metal is selected from the group consisting of Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the metal comprises cobalt. In some embodiments, the metal comprises chromium. In some embodiments, the metal comprises nickel. In some embodiment the metal is any metal that can be hyperaccumulated by a hyperaccumulator plant. \|[0053] In some embodiments, the weatherable rock comprises a magnesium-bearing silicate mineral. In certain embodiments, the magnesium-bearing silicate mineral is in the olivine mineral group. In certain embodiments, the magnesium-bearing silicate mineral is in the serpentinite mineral group. In other variations, any combination of suitable weatherable rocks described herein may be used. \|[0054] In some embodiments, providing the weatherable rock comprises mining the weatherable rock. In some embodiments, providing the weatherable rock further comprises mechanically processing the weatherable rock to reduce the particle size of the weatherable rock to between about 1 pm and about 10 cm. In some embodiments, providing the weatherable rock further comprises admixing the weatherable rock with one or more additional growing media including, for example, soil. \|[0055] In another aspect, provided herein is a method that utilizes plants that are not only tolerant to serpentine, but that evolved especially to live in high alkalinity (e.g., high pH) soils, composed of high percentages of low nutrient and metal heavy soils. These plants that typically take up nickel as a means of protection can be utilized to produce commercial yields of nickel. In certain aspects, provided is a method to bring fresh serpentine-containing rock from nearby quarries, utilizing mechanical activation to grind them to particles, for example micron-sized particles, to increase the reactive surface area, then transported to fields where nickel hyperaccumulating plants have been planted to capture the nickel release from the soil, and also accelerate the release of magnesium ions from the crystal lattice of the serpentine in order to increase the amount of carbon sequestered when those ions run off to the ocean. The methods provided herein overcome the previous blockers that prevented the deployment of terrestrial enhanced weathering for the purposes of carbon removal, and by increasing the revenue streams available to the process are able to make direct and intentional phytomining possible. The methods provided make phytomining a primary mining technique. In some variations, the methods can also use tailings, waste, or overburden from traditional nickel mines. In certain variations, the methods involve actively grinding minerals to below a certain size in order to specifically increase the reactive surface area. Further, in some variations, direct irrigation can be utilized to both enhance the weathering rate, and increase the plant growth, the plant then releases acids that further break down the rocks, releasing magnesium that leads to carbon removal and drawing nickel into the plants, preventing its release into the environment. \|[0056] In some variations of the foregoing, the chemical weathering process results in the formation of new soil minerals. In certain variations of the foregoing, the chemical weathering process results in fully weathered rock. In some embodiments, the weathering process results in fully weathered rock within about 20 years; or between 1 year and 20 years; or within about 1 year, about 2 years, about 3 years, about 4 years, about 5 years, about 6 years, about 7 years, about 8 years, about 9 years, about 10 years, about 11 years, about 12 years, about 13 years, about 14 years, about 15 years, about 16 years, about 17 years, about 18 years, about 19 years, or about 20 years. \|[0057] With reference to FIG. 1, depicted is an exemplary process 100 for obtaining metal using weatherable rock and phytomining. Step 102 involves mechanically grinding a weatherable rock to provide a particulate weatherable rock composition. In step 104, the particulate weatherable rock composition is combined with a soil to provide a weatherable rock-enriched soil. In step 106, a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil is grown. Then, in step 108, the metal hyperaccumulator plant is harvested. In step 110, the harvested metal hyperaccumulator plant is processed using any suitable techniques or methods known in the art to provide a substantially pure metal. In some variations of the process, step 110 may be optional. For example, in certain variations, the process described herein does not require harvesting of the metal from the plant to obtain a substantially pure metal. In other variations, the process further includes harvesting of the metal from the plant to obtain a substantially pure metal.\|[0058] Thus, in some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising magnesium, and a metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil; harvesting the metal hyperaccumulator plant; and processing the harvested metal hyperaccumulator plant to provide a substantially pure metal. In some embodiments, processing the harvested metal hyperaccumulator plant comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide a substantially pure metal by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide a substantially pure metal may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 20% by weight of magnesium and 0.1% by weight of the metal. In some embodiments, the metal-enriched ash comprises at least 5% of the metal by weight. \|[0059] In some embodiments, provided is a method for preparing one or more metals comprising mechanically grinding a weatherable rock comprising magnesium, and one or more metals to provide a particulate weatherable rock composition; either combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil or using the particulate weatherable rock composition directly as a weatherable rock- enriched soil without combining it with any additional media; growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil, wherein each of the one or more plants is a hyperaccumulator of at least one of the one or more metals; harvesting the one or more metal hyperaccumulator plants; and processing the one or more harvested metal hyperaccumulator plants to provide one or more substantially pure metals. In some embodiments, processing the one or more harvested metal hyperaccumulator plants comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide one or more substantially pure metals by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide one or more substantially pure metals may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 20% by weight of magnesium and 0.1% by weight of each of the one or more metals. In some embodiments, the metal-enriched ash comprises at least 5% of each of the one or more metals by weight.\|[0060] In some embodiments, provided is a method for obtaining one or more substantially pure metals comprising mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium and at least 0.1% by weight of each of the one or more metals to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil, wherein each of the one or more plants is a hyperaccumulator of at least one of the one or more metals; harvesting the one or more metal hyperaccumulator plants; and processing the one or more harvested metal hyperaccumulator plants to provide one or more substantially pure metals. \|[0061] In some variations, substantially pure metal refers to a metal that is at least 90%, at least 95%, at least 96%, at least 97%, at least 98%, at least 99%, at least 99.9%, at least 99.99%. at least 99.999%, or at least 99.9999% pure by weight. \|[0062] In some embodiments, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the metal hyperaccumulator plant is growing. In some embodiments, about 10% of the Mg by weight is weathered per year. In some embodiments, about 90% of the Mg by weight is weathered per month. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated over a period of about 20 years. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated over a period of less than about 20 years. In any of the foregoing embodiments, the weight of Mg2+ refers to the weight of the magnesium component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts that the Mg2+ is a part of. \|[0063] In some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising calcium and a metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil; harvesting the metal hyperaccumulator plant; and processing the harvested metal hyperaccumulator plant to provide a substantially pure metal. In some embodiments, processing the harvested metal hyperaccumulator plant comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide a substantially pure metal by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide a substantially pure metal may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 10% by weight of calcium and at least 0.1% by weight of the metal. In some embodiments, the metal-enriched ash comprises at least 5% of the metal by weight. \|[0064] In some embodiments, Ca2+ is leached at a rate of at least 1% by weight of the total Ca2+ in the weatherable rock per year from the weatherable rock-enriched soil while the metal hyperaccumulator plant is growing. In some embodiments, about 10% of the Ca by weight is weathered per year. In some embodiments, about 90% of the Ca by weight is weathered per month. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated over a period of about 20 years. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated over a period of less than about 20 years. In any of the foregoing embodiments, the weight of Ca2+ refers to the weight of the calcium component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts that the Ca2+ is a part of. \|[0065] In some embodiments, the rate at which Mg2+ is leached is measured by measuring the concentration of the Mg2+ in the water used to irrigate the hyperaccumulator plant. In some embodiments, the rate at which Ca2+ is leached is measured by measuring the concentration of Ca2+ in the water used to irrigate the hyperaccumulator plant. \|[0066] In some variations of the foregoing, the weatherable rock comprises between 0.01% and 20% of the metal by weight. In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of the metal by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of the metal. \|[0067] In some embodiments, the metal comprises Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the metal comprises a rare earth metal. In some embodiments, the metal comprises nickel. In some embodiments, the metal comprises cobalt. In some embodiments, the metal comprises chromium. In some embodiments, the metal is a metal that can be hyperaccumulated by a hyperaccumulator plant. In some embodiments, the metal is a metal found in a weatherable rock. In some embodiments, the metal is a metal found in a weatherable rock that can be hyperaccumulated by a hyperaccumulator plant. \|[0068] In some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising magnesium and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; liberating nickel from the weatherable rock by subjecting the weatherable rock-enriched soil to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein acid is not added to the weatherable rock- enriched soil; growing a plant that is a hyperaccumulator of nickel in the weatherable rock- enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide substantially pure nickel. \|[0069] In some embodiments, the amount of carbon dioxide emitted from the weathering of the weatherable rock is less than amount of carbon dioxide sequestered from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide emitted from the weathering of the weatherable rock, harvesting the nickel hyperaccumulator plant, and processing the harvested nickel hyperaccumulator plant is less than amount of carbon dioxide sequestered from the weathering of the weatherable rock. \|[0070] In some embodiments, provided is a method for preparing nickel metal comprising mechanically grinding a weatherable rock comprising magnesium, and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel. In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash and refining the nickel-enriched composition to provide a substantially pure nickel by weight. In some embodiments, processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 10% by weight of magnesium and at least 0.1% by weight of nickel. In some embodiments, the nickel-enriched ash comprises at least 5% nickel by weight. \|[0071] In some variations of the foregoing, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the nickel hyperaccumulator plant is growing. \|[0072] In some variations of the foregoing, the weatherable rock comprises between 5% and 60% Mg by weight. In some embodiments, the weatherable rock comprises between 25% and 50% Mg by weight. In some embodiments, the weatherable rock comprises about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, or about 70% Mg by weight. \|[0073] In some variations of the foregoing, the weatherable rock comprises between 5% and 60% Ca by weight. In some embodiments, the weatherable rock comprises between 25% and 50% Ca by weight. In some embodiments, the weatherable rock comprises about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, or about 70% Ca by weight. \|[0074] In some variations of the foregoing, the weatherable rock comprises between 0.01% and 20% of nickel by weight. In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of nickel by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of nickel. \|[0075] In some variations of the foregoing, the weatherable rock comprises nickel and Mg. In some embodiments, the weatherable rock comprises between 0.01% and 25% of nickel by weight and between 5% and 60% of Mg by weight. In some embodiments, the weatherable rock comprises between 0.01% and 25% of nickel by weight and between 25% and 50% of Mg by weight. \|[0076] In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of nickel by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of nickel. \|[0077] In some variations of the foregoing, the nickel-enriched ash composition comprises between 1% and 99.8% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 1% and 35% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 1% and 30% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 30% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 20% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 15% nickel by weight. In some embodiments, the nickel- enriched ash composition comprises about 0.1%, about 0.5%, about 1%, about 1.5%, about 2%, about 2.5%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, or about 40% nickel by weight. \|[0078] In some variations of the foregoing, refining the nickel-enriched composition provides a nickel that is at least 15%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 98%, at least 99%, at least 99.9%, at least 99.9%, at least 99.99%, at least 99.999%, or at least 99.9999% pure by weight. In some embodiments, refining the nickel-enriched composition provides a nickel that is between 15% and 100% pure by weight. \|[0079] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprises drying the nickel hyperaccumulator plant to provide a dried biomass composition, crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a nickel-enriched ash composition. In some embodiments, the ashing is performed at a temperature of about 500 °C. \|[0080] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises directly leaching the harvested nickel hyperaccumulator plant to provide a leachate; purifying the leachate to provide a Ni-enriched leachate; and further processing the Ni-enhanced leachate to provide a substantially pure nickel. In some embodiments, the direct leaching is performed using a hydrothermal process. In some embodiments, the direct leaching is performed in acid. In some embodiments, the acid is sulfuric acid. In some embodiments, the acid is hydrochloric acid. In some embodiments purifying the leachate comprises purifying the leachate using column chromatography. In some embodiments purifying the leachate comprises purifying the leachate using solvent extraction. In some embodiments purifying the leachate comprises purifying the leachate using ion exchange chromatography. In some embodiments, further processing the Ni-enhanced leachate comprises electrowinning the nickel. \|[0081] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash, leaching the nickel-enriched ash composition to provide a leachate, treating the leachate to provide ammonium Ni sulfate hexahydrate (ANSH), and processing the ANSH to obtain a substantially pure nickel. In some embodiments, the leaching is performed in acid. In some embodiments treating the leachate comprises neutralizing the leachate using a base to provide a first treated leachate, adding a fluoride source to the first treated leachate to provide a second treated leachate, adding ammonium sulfate to the second treated leachate to provide a third treated leachate, and drying the third treated leachate to provide ANSH. In some embodiments, the base is Ca(OH)2. In some embodiments, the fluoride source is NaF. In some embodiments, treating the leachate comprises purifying the ANSH via recrystallization. \|[0082] In some embodiments, provided is a method for preparing nickel catalysts comprising mechanically grinding a weatherable rock comprising magnesium, and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide nickel catalysts. In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash, leaching the nickel-enriched ash to provide a leachate, and further processing the leachate to provide nickel catalysts. In some embodiments, the ashing is performed at a temperature of 500 °C. In some embodiments, the leaching is performed in acid. In some embodiments, the acid is hydrochloric acid. In some embodiments, further processing the leachate to provide nickel catalysts comprises dispersing the leachate onto montromorillonite K10. In some embodiments, the weatherable rock comprises at least 10% by weight of magnesium and at least 0.1% by weight of nickel.\|[0083] In some embodiments, the amount of carbon dioxide sequestered is on the tonne scale for every tonne of nickel metal that is produced. In some embodiments, at least 1 tonne, at least 5 tonnes, at least 10 tonnes, at least 20 tonnes, at least 30 tonnes, or at least 40 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. In some embodiments, between 1 tonne and 100 tonnes, or between 10 tonnes and 100 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. In some embodiments, between 100 tonnes and 500 tonnes, or between 300 tonnes and 500 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. \|[0084] In some embodiments, the weatherable rock comprises an ultramafic rock. In some embodiments, the weatherable rock comprises serpentine. In some embodiments, the weatherable rock comprises serpentinite. In some embodiments, the weatherable rock comprises olivine. In some embodiments, the weatherable rock contains less than 1% by weight of nickel. In some embodiments, the weatherable rock contains a metal that can be hyperaccumulated by a hyperaccumulator plant. \|[0085] In some embodiments, the method further comprises mining the weatherable rock. In other embodiments, the method further comprises transporting the mined weatherable rock from a mining location to a grinding location. \|[0086] In some embodiments, mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock. In some embodiments, the energy used to mechanically grind the rock comes from renewable sources. \|[0087] In some embodiments, the particulate weatherable rock composition has an average particle size between about 1 pm and about 10 mm, between about 1 pm and about 10 cm, between about 1 pm and about 20 cm, between about 1 pm to about 5 mm, between about 1 pm to about 3 mm, or between about 100 pm to about 3 mm. \|[0088] In some embodiments, the weatherable rock-enriched soil comprises between 10% and 100%, between 70% and 100%, between 70% and 90%, between 70% and 80%, or between 80% and 90% particulate weatherable rock composition by weight. In certain embodiments, the weatherable rock-enriched soil comprises about 30%, about 40%, about 50%, about 60%, about 70%, about 80%, about 90%, or about 100% particulate weatherable rock composition by weight.\|[0089] In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of silicate rocks. In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of serpentinite rocks. In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of olivine rocks. In some embodiments, natural weathering of serpentinite rocks results in weatherable rock-enriched soil with high nickel concentrations. \|[0090] In some embodiments, the nickel hyperaccumulator plant is a plant belonging to the genus Odontarrhena. In some embodiments the plant belongs to the genus Alyssum. In some embodiments the plant belongs to the family Brassicacaea. In some embodiments the plant belongs to the genus Bornmuellera. In some embodiments the plant belongs to the genus Thlaspi. In some embodiments, the plant is Alyssum Murale. In some embodiments, the plant is of the genus Odontarrhena. In some embodiments, the plant is Odontarrhena chalcidica. In some embodiments, the plant is Odontarrhena decipiens. In some embodiments, the plant is Berkheya coddii. In some embodiments, the plant is B. emarginata. In some embodiments, the plant is Stackhousia tryonii. In some embodiments, the plant is Phyllanthus balgooyi. In some embodiments, the plant is Rinorea bengalensis. In some embodiments, the plant may be a tree, bush, or vine. In some embodiments, the plant is a genetically modified plant. In some embodiments, the plant is any plant capable of hyperaccumulating a metal found in a weatherable rock. In some embodiments, the plant is any plant capable of hyperaccumulating nickel. In some embodiments, the plant is any hyperaccumulator plant species of the class known as a hypernickelophores, containing more than 1,000 pg Ni g 1. \|[0091] In some embodiments, the nickel hyperaccumulator plant is grown inside of a greenhouse. In some embodiments, the nickel hyperaccumulator plant is grown inside of a vertical farm. In some embodiments, the nickel hyperaccumulator plant is grown hydroponically. In some embodiments, the nickel hyperaccumulator plant is grown under a polyethylene film (e.g., a polytunnel). \|[0092] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the weathering rate of the weatherable rock. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the efficiency of nickel uptake by the plant. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the weathering rate of the weatherable rock and the efficiency of nickel uptake by the plant. \|[0093] In some embodiments, the environmental conditions of the weatherable rock- enriched soil are controlled to cause the weatherable rock to undergo a chemical weather process at an accelerated rate relative to natural chemical weathering environmental conditions. In some embodiments, the conditions cited above comprise growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil. In some embodiments, the conditions comprise growing one or more metal hyperaccumulator plants in a weatherable rock-enriched soil and continuously irrigating the one or more metal hyperaccumulator plants using a drip irrigation system. In some embodiments, the temperature, pH, irrigation, or bioactivity of the weatherable rock-enriched is controlled. \|[0094] In some embodiments, the rate of weathering of the weatherable rock is between about 0% and about 40% by mass of the weatherable rock between about 12 months and about 72 months from the date of combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil and planting the hyperaccumulator plant in the weatherable rock-enriched soil. Any suitable methods known in the art may be used to determine the rate of weathering of the weatherable rock. For example, in one variation, the foregoing rates of weathering may be calculated using the Arrhenius equation. \|[0095] In some embodiments, the weathering rate is calculated by measuring the accumulation of rock-derived cations (e.g., Ca, Mg, Na, and K) in plant, soil, and/or aqueous effluent associated within a certain plot of land and subtracting the baseline amount of the corresponding cation measured in a corresponding control plot. For example, the net accumulation of Ca-cations due to mineral dissolution of weatherable rock can be calculated by subtracting the amount of Ca-cations measured in a control plot from the total amount of Ca-cations calculated by totaling the amount of Ca-cations in the water and/or effluent, the Ca-cations in plant tissues, and Ca-cations in the soil cation exchange pool. The amount of Ca-cations attributable to the weathering of weatherable rock can then be converted into spatially-averaged cation weathering rates (per unit of land area) or rates related to mineral surface area. In some embodiments, the weatherable rock is calculated in the number of moles of calcium, magnesium, sodium, and/or potassium released from the weatherable rock material into the soil per hectare of treated land per annum.\|[0096] In some embodiments, the weathering rate of the weatherable rock increases when the average particle size of the weatherable rock decreases. \|[0097] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to increase the weathering rate of the weatherable rock. In some embodiments, the environmental parameter that is optimized to increase the weathering rate of the weatherable rock is temperature. In some embodiments, the temperature of the surrounding air (e.g., climate) is increased to increase the weathering rate of the weatherable rock. In some embodiments, the temperature of the topsoil (e.g., where the weatherable rock is admixed into the soil) is increased to increase the weathering rate of the weatherable rock. In some embodiments, the amount of irrigation of the soil admixed with the weatherable rock is increased to increase the weathering rate of the weatherable rock. In some embodiments, the pH of the soil admixed with the weatherable rock is increased to decrease the weathering rate of the weatherable rock. In some embodiments, the pH of the soil admixed with the weatherable rock is decreased to increase the weathering rate of the weatherable rock. \|[0098] In some embodiments, the weathering rate of the weatherable rock is increased by increasing the amount of biological activity of the soil admixed with the weatherable rock. In certain embodiments, the increased biological activity of the soil is measured by the amount of carbon dioxide produced by the microbes per a given amount of the soil. In certain embodiments, the increased biological activity of the soil is measured by the amount of nitrogen-cycling and secretion of organic acids by plant roots and mycorrhizal fungi present in the soil. \|[0099] In some embodiments, increasing the concentration of Mg2+ ions in the soil admixed with the weatherable rock increases the weathering rate of the weatherable rock. In some embodiments, increasing the concentration of Ca2+ ions in the soil admixed with the weatherable rock increases the weathering rate of the weatherable rock. In certain variations, higher soil Ca and Mg content may decrease the weathering rate of rock material added to the soil, because chemical conditions in the groundwater may approach saturation for certain Ca- (and Mg-) bearing minerals. \|[0100] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the accumulation of nickel by the plant. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the growth rate of the plant. In some embodiments, the humidity, temperature, or lighting of the environment in which the nickel hyperaccumulator plant is grown are controlled. In some embodiments, the nickel hyperaccumulator plant is grown in an outdoor field. \|[0101] In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to maximize the accumulation of nickel by the hyperaccumulator plant. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is between about 5 tonnes and 300 tonnes. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is between about 10 tonnes and 50 tonnes. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is about 37 tonnes. \|[0102] In some embodiments, the amount of nickel accumulated by a nickel hyperaccumulator plant increases proportionally with the amount of weatherable rock mixed into the soil in which the plant is grown. In some embodiments, increasing the amount of weatherable rock mixed in the soil does not result in an increase in the amount of nickel accumulated by a hyperaccumulator plant growing in the soil. In certain embodiments, high amounts of weatherable rock mixed into the soil result in high alkaline (e.g., high pH) soils which can negatively impact the mobility of the one or more metals released from the weatherable rock during the weathering process. \|[0103] In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown and the environmental conditions under which the hyperaccumulator plant is grown are optimized to control the pH of the soil. In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to control the pH of the soil. In some embodiments, an increase in the pH of the soil decreases the mobility of the one or metals released by the weatherable rock mixed in the soil. In some embodiments, decreased mobility of the one or more metals in the soil results in lower accumulation of the metals by a hyperaccumulator plant of the same metal growing in the soil. In some embodiments, an increase of the pH of the soil decreases the amount of metal accumulated by the hyperaccumulator plant growing in the soil, the mobility of the one or metals released by the weatherable rock, or both. \|[0104] In some embodiments the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to maximize the growth rate of the hyperaccumulator plant. \|[0105] In some embodiments, at least 5 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, at least 10 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 10 tonnes and 100 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 5 tonnes and 10 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 25 tonnes and 50 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 35 tonnes and 40 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 100 tonnes and 200 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, about 150 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 400 tonnes and 800 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. . In some embodiments, about 600 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. \|[0106] In some embodiments, at least about 20 tonnes of nickel hyperaccumulator biomass is grown per hectare. In some embodiments, at least about 400 kg, at least about 500 kg of nickel, at least about 600 kg, at least about 700 kg, at least about 800 kg, at least about 900 kg, or at least about 1,000 kg of nickel is produced per hectare. In other variations, between about 100 kg and 5000 kg, or between 250 kg and 1000 kg, or between 400 kg and 1000 kg of nickel is produced per hectare.\|[0107] In some embodiments, between about 5 tonnes and about 50 tonnes, between about 100 tonnes and about 700 tonnes, between about 500 tonnes and about 700 tonnes, between about 100 tonnes and about 600 tonnes, between about 200 tonnes and about 600 tonnes, between about 300 tonnes and about 600 tonnes, between about 400 tonnes and about 600 tonnes, between about 500 tonnes and about 600 tonnes, between about 100 tonnes and about 500 tonnes, between about 200 tonnes and about 500 tonnes, between about 300 tonnes and about 500 tonnes, between about 400 tonnes and about 500 tonnes, between about 100 tonnes and about 400 tonnes, between about 200 tonnes and about 400 tonnes, between about 300 tonnes and about 400 tonnes, between about 100 tonnes and about 300 tonnes, between about 200 tonnes and about 300 tonnes, or between about 100 tonnes and about 200 tonnes of weatherable rock are mixed into the soil for every hectare on which the hyperaccumulator plant is grown. In some embodiments, about 500 tonnes about 600 tonnes, or about 700 tonnes of weatherable rock are mixed into the soil for every hectare on which the hyperaccumulator plant is grown. \|[0108] In some embodiments, the amount of carbon dioxide sequestered is proportional to the number of Mg2+ ions liberated from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide sequestered per hectare is proportional to the number of Mg2+ ions liberated from the weathering of the weatherable rock mixed into the soil for every hectare. \|[0109] In some embodiments, the amount of carbon dioxide sequestered is proportional to the number of Ca2+ ions liberated from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide sequestered per hectare is proportional to the number of Ca2+ ions liberated from the weathering of the weatherable rock mixed into the soil for every hectare. \|[0110] In some embodiments, the nickel hyperaccumulator plant is harvested mechanically. In some embodiments, the nickel hyperaccumulator plant is harvested manually. In some embodiments, the nickel hyperaccumulator plant is harvested by an automated process. \|[0111] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil. In some embodiments, the plant is irrigated using a drip irrigation system. In some embodiments, the plant is irrigated using sprinkler systems. In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises intermittently irrigating the weatherable rock-enriched soil. In some embodiments, the plant is irrigated using a flood irrigation approach. In some embodiments, the plant is irrigated using traditional irrigation. \|[0112] In some embodiments, the pH of the weatherable rock-enriched soil is above 7. In some embodiments, the pH of the weatherable rock-enriched soil is between 7 and 14. In some embodiments, the pH of the weatherable rock-enriched soil is between 5 and 14. In some embodiments, increasing the content of the weatherable rock of the weatherable rock- enriched soil increases the pH of the soil. \|[0113] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprise drying the nickel hyperaccumulator plant to provide a dried biomass composition; crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a nickel-enriched composition. \|[0114] In some embodiments, the method further comprises quantifying the amount of carbon dioxide that is released or sequestered in one or more steps of any of the methods described herein. In some embodiments, the amount of carbon dioxide released or sequestered by a process is measured directly. In some embodiments, the amount of carbon dioxide released or sequestered by a process is measured using a proxy. In some embodiments, the quantity of Mg2+ is used as a proxy to quantify the amount of carbon dioxide sequestered by chemical weathering of the weatherable rock. \|[0115] In another aspect, provided herein is nickel metal prepared according to any of the methods described above. \|[0116] In another aspect, provided herein is a processed nickel composition comprising a substantially pure nickel, and one or more of the following: Nickel rich ashes also containing K, Ca, oxides (e.g., NiO, MgO), carbonates (e.g., K2CO3, CaCO3, K2Ca(CO3)2), K2SO4, precipitated gypsum, low-mass carboxylic acids, Ni-bearing organic and inorganic compounds. Ni-based compounds such as NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, Ni oxalate, and Ni sulfate. In some variations of the foregoing, the processed nickel composition is at least 15%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 98%, at least 99%, at least 99.8%, at least 99.9%, at least 99.99%, at least 99.999%, or at least 99.9999% pure by weight. In some embodiments, the processed nickel composition is between 15% and 100% pure by weight. \|[0117] In another aspect, provided herein is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: Nickel rich ashes also containing K, Ca, oxides (e.g., NiO, MgO) and carbonates (e.g., K2CO3, CaCCh, KiCa CCh ), K2SO4, precipitated gypsum, low-mass carboxylic acids, Ni-bearing organic and inorganic compounds. Ni-based compounds such as NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, Ni oxalate, and Ni sulfate. In some embodiments, provided herein is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: Ca, Fe, K, Mg, carbonates (e.g., K2CO3, CaCOs, or K2Ca(CO3 ), P, plant cells, C, H, N, O, hydroxyapatite, oxy -hydroxyapatite, or oxides (e.g., NiO, CaO, MgO, or MgNiO2). In some embodiments, the nickel-enriched ash comprises between 5% and 100% nickel by weight. \|[0118] In any of the foregoing embodiments, the weight of nickel refers to the weight of the nickel component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts, respectively, that the nickel is a part of. \|EXAMPLES \|[0119] The presently disclosed subject matter will be better understood by reference to the following Examples, which are provided as exemplary of the invention, and not by way of limitation. \|Example 1: Assessment of weathering rates for different soil and plant configurations\|[0120] Samples of O. decipiens (a close relative to the hyperaccumulator known in the art as O. chalcidica or A. morale) were shipped to a testing facility. There, the seeds were separated from the remainder of the plant biomass, soaked in water to prepare them for germination, and germinated. The germinated seeds were observed to have root systems. Separately, a sample of serpentinite rock was obtained, and was ground into a fine powder, herein referred to as “serpentine soil”. \|[0121] Nine sample planters were prepared, with each planter containing a specific ratio of serpentine soil to potting soil (including both pure potting soil and pure serpentine soil). Seeds of the hyperaccumulator plants were planted in eight of the nine planters, and one planter was left with no seeds, as a control. Additionally, NPK hydroponic fertilizer was added in different concentrations to the continuous, closed-loop irrigation systems of two of the planters. The experimental conditions for each planter are illustrated in FIG. 2. \|[0122] Because Mg2+ is released in the weathering reaction of serpentine, the quantity of Mg2+ leached from the soils in each planter was used as a proxy for the rate of weathering that occurred under each condition. Over the course of 4 months, the total concentration of Mg2+ leached into the closed-loop irrigation system was measured for each of the nine planter conditions shown in FIG. 2. The results of these measurements are shown in FIG. 3. Surprisingly, it was found that quantity of Mg2+ leached by the soil mixtures increased over time as the plants grew. Further, the rate of weathering, as assessed using Mg2+ leaching as a proxy, was found to correlate to plant biomass growth. \|Example 2: Field-scale enhanced rock weathering experiment \|[0123] A field-scale trial was employed to investigate the synergistic combination of nickel phytomining and enhanced weathering. The principal aim of this experiment was to evaluate the scope for nickel extraction by the hyperaccumulator plant Odontarrhena decipiens and to quantify the carbon capture potential of crushed serpentinite rock added to the naturally occurring serpentine agricultural soil. \|[0124] A 112 m x 168 m field site was selected for this trial based on aerial photography and ground observations. Four permanent reference points for determining precise locations were established by cementing steel posts into the ground at the comers of the field site. The area was then partitioned into four equally-sized rectangular blocks, each measuring 56 m x 84 m. A scale diagram of the randomized complete block design used in the trial is shown in FIG. 4. These blocks represent replicates, such that each block contained eight randomized 12 m x 18 m plots (one for each of the eight rock treatments) separated by an 8 m margin of untreated land. The amount of rock treatment added to each plot as measured in tonnes of serpentinite rock per hectare is shown in FIG. 4. The randomized complete block design accounts for the effects of extraneous variables (e.g. hydrological gradients across the site) and hence, mitigates bias caused by inherent variation. \|[0125] The entire field site was tilled prior to the trial. Crushed serpentinite rock was sourced from a nearby quarry and applied by hand to the soil surface of each plot at rates ranging from 9.375 to 600 tonnes per hectare, whereby the next higher rate was set to be double the previous as illustrated in FIG. 4. Each block also contains a ‘control’ treatment where no serpentinite rock is added (i.e. 0 tonnes per hectare), against which all other treatments were compared statistically. The applied rock material was incorporated into the soil to an approximate depth of 150 mm using a rotavator. One-year-old Odontarrhena decipiens specimens were then transplanted into each plot, in thirteen rows with 1 m rowspacing and 0.5 m spacing between the individual plants. Organic fertilizers, pesticides, and fungicides were added to the experimental plots to ensure baseline crop performance and mitigate pest/pathogen interference in all treatments. \|[0126] At the beginning of the experiment, over a hundred mesh bags were filled with 0.4 g of crushed serpentinite and buried in the plots at soil depths between 50-200 mm. Retrieval of the grains from these bags at the end of the trial permits the direct assessment of mineral weathering through X-ray analysis. \|Soil sample collection and measurements \|[0127] Before applying the serpentinite rock material, fifteen baseline soil samples were collected from each block using a steel auger and following a W-shaped sampling pattern. These initial (pre-planting, pre-rock application) soil samples are taken from three depths: 0- 0.3 m, 0.3-0.6 m, and 0.6-0.9 m. Soils are then passed through a 2 mm mesh size sieve, air dried, and tested for the following physical and chemical parameters: pH (in H2O and IM KC1); organic matter and humus %; plant-available nitrogen, phosphorus and potassium; soil texture (sand/silt/clay %); cation exchange capacity; and, total and plant-available Ca, Mg, K, Na, Fe, Cd, Co, Cr, Cu, Mn, Ni, Pb, and Zn. Further soil samples were collected monthly from each of the thirty-two experimental plots and tested for pH, electrical conductivity, cation exchange capacity, and plant-available cations. These data were used to monitor changes in the concentrations of plant-available nutrients and nickel over time, and to estimate rock weathering and carbon dioxide capture rates via a conventional mass balance approach, in combination with novel quantification methods. \|Plant sample collection and measurements \|[0128] Aboveground plant tissues are harvested from all plots after a suitable time (e.g., approximately 6-8 months) after the trial began. Plant materials are dried and weighed to determine crop yields, and ground for analysis of nutrients and metals. These data are used to measure the efficiency of nickel uptake by the hyperaccumulator plants, and to evaluate the correlation between rock application and nickel uptake rates. Moreover, values for total uptake of calcium, magnesium, potassium and sodium are fed into mass budget calculations for carbon capture quantification. \|[0129] Aboveground plant tissues were harvested from five different mature hyperaccumulator plant specimens randomly selected from all plots after a suitable time (e.g., approximately 6-8 months) after the trial began. Plant samples were washed with distilled water, dried in a forced-air oven at 60 °C for 48 hours, and powdered separately using a laboratory grinding mill. These plant samples were used to determine total heavy metal concentrations in the plant tissues. \|Soil pH and electrical conductivity measurements \|[0130] The pH and the electrical conductivity (EC) of the soil samples determined using a Combined Conductivity /pH Meter equipped with a temperature input, which internally corrects for the effect of temperature on measured values. pH and EC were standardized using a 3-point calibration protocol with certified reference solutions (buffers at pH 4.00, 7.00, and 14.00; EC standards at 12.88 mS, 1413 pS, and 84 pS). To streamline the measurements, pH and EC were tested sequentially from the same sample. For each soil sample, 15.0000 ± 0.0005 g of soil was weighed into a 50 mL polypropylene centrifuge tube and combined with 30.0000 ± 0.0150 mL of ultrapure water (resistivity of 18.2 MQ-cm at 25 °C). The tubes were stoppered, agitated on a rotary shaker for 3 minutes, unstoppered and then left to equilibrate with the atmosphere for 30 minutes. An additional three replicates of control soil (initial/baseline soil containing no additives) were prepared and used to precondition the pH and conductivity electrodes prior to analysis of the experimental samples. This preconditioning process shortens the timescales for stable measurements and mitigates measurement error in the first few experimental samples (e.g. due to contamination with trace amounts of buffer solution). To obtain pH measurements, the pH electrode was swirled into the soil-water mixture’s supernatant for 10 seconds, and then gently released into the slurry until the instrument identified that a stable pH reading was achieved (or 3 minutes after initial insertion, where stabilization was not achieved). pH measurements were recorded to 0.001 pH units, and the electrode was rinsed thoroughly with ultrapure water between samples. To obtain EC measurements, the conductivity electrode was inserted into the soilwater mixture’s supernatant and held until the instrument indicated that a stable EC reading was achieved (or 1 minute after initial insertion, where stabilization was not achieved). EC measurements were recorded to four significant figures, and the electrode was rinsed thoroughly with ultrapure water between samples. \|Soil analysis methods for total heavy metals \|[0131] The soil samples were tested for total heavy metals by first drying a test portion of the soil and reducing the grain size of the soil to below a particle size of 250 microns. Each test portion of the soil was then weighed (0.5 g to 1.0 g based on dry mass) and transferred to a microwave extraction vessel. A few drops of water were then added to the extraction vessel before adding a HC1 and nitric acid solution and mixing well. The temperature of the extraction mixture was increased at a rate of approximately 10 °C/min to 175 ± 5 °C using a microwave digestion system. The amount of total Ni in the soil samples was then determined using ICP-OES. \|Availability ofNi with Mehlich-1 digestion \|[0132] The soil samples were prepared by mixing 5 g of the soil samples with 20 mL of a Mehlich-1 extraction solution consisting of a mixture of HC1 and H2SO4. The mixture was then stirred for 5 min at 180 cycles/min after which the suspension was allowed to rest for 16 h before decanting off the supernatant The total amount of Ni in the soil samples was then determined by testing an aliquot of the supernatant using ICP-OES. \|Other analytical methods \|[0133] It should be understood that one or more additional techniques may be used to determine the amount of Ni in the soil, the amount of rock-derivable cations in the tissue of the hyperaccumulator plants or the soil, the amount of heavy metals in the tissue of the hyperaccumulator plants or the soi, the pH of the soil, the electrical conductivity of the soil, and other aspects of the weatherable rock, soil, and hyperaccumulator plants, including quantification of the weathering rate. For example, X-ray fluorescence analysis of weathered rock material (retrieved from mesh bags buried in the plots) is used to quantify changes in grain surface chemistry. These data provide an independent method for mineral weathering rate quantification. The loss of cations from the added rocks may serve as a proxy for the accumulation of cations released from this process in the plant and soil. \|Determination of total heavy metal and Ca, Mg, K concentrations in plants with digestion\|[0134] Aboveground plant tissues were digested in an acid solution (HNO3 65% and H2O2 30%) using a microwave digestion system to determine total heavy metal concentrations in plants. A sample of the plant matter (300 mg) was mixed with 2 mL of HNO3 and 2 mL of H2O2, stirred for at least 20 min, and then digested using a microwave digestion system. Plant tissue samples calibration curves were plotted from Ni concentrations of 2, 4 and 6 mg/L. The solution was diluted 20 times. The amount of Ni in the plant tissue samples was then determined using ICP-OES. \|Results and Analysis \|[0135] Approximately 8 months after the trial began, representative soil samples were collected from the plots for analysis. As shown in FIG. 5, increasing serpentinite application rates resulted in increasing soil pH. Moreover, application rates above 0.9375 kg m 2 resulted in statistically significant increases in soil pH with respect to the control soils, where no serpentinite rocks were added, which is evidence of chemical weathering of the added serpentinite rock. Surprisingly, soil pH continued to increase with increasing application rates, and rose substantially to the highest recorded level at the highest application rate (60 kg m 2) as shown in FIG. 5. Chemical weathering of the added alkaline minerals (e.g. serpentinite rock) will lead to carbon dioxide sequestration. Enhanced weathering of the added rock material is also supported by evidence of elevated soil electrical conductivity (EC) following rock applications as shown in FIG. 6. Higher EC indicates the release of cations due to rock dissolution, and similarly represents evidence for chemical weathering of the serpentinite rock applied to the soil. This chemical weathering leads to carbon dioxide sequestration. \|[0136] Amendment of soils with serpentinite rock also resulted in higher nickel uptake into the tissues of the hyperaccumulator plants as compared to the hyperaccumulator plants grown in the control soils, with the highest nickel yields observed in soils amended with 3.75 to 15 kg m 2 of serpentinite rock as shown in FIG. 7. The mean total Ni yield from the hyperaccumulator plants was calculated by multiplying the (dry) biomass yield by the (dry) biomass Ni concentration. Mean total Ni yields from the hyperaccumulator plants ranged from around 1.4 g Ni m 2 (14 kg Ni ha 1) in the control plots to a peak of about 2.5 g Ni m 2 (25 kg Ni ha 1) in the plots treated with 15 kg m 2 (150 t ha 1) of serpentinite rock. Plants grown on soils with elevated pH will typically accumulate less nickel. Surprisingly, nickel yields increased in the soils amended with 3.75 to 15 kg m 2 of serpentinite rock, which implies that the combination of enhanced weathering of serpentinite and nickel hyperaccumulators realized a synergistic benefit. Overall, this data indicates mass transfer of Ni from the applied serpentinite rock into the tissues of the hyperaccumulator plants. \|[0137] Timeseries data for soil-extractable Ni was determined by a Mehlich 1 extraction procedure and confirms that soil concentrations increased in all plots treated with serpentinite rock between when the trial began (0 m) and the following spring (~5 m), when the hyperaccumulators would have exhibited low primary production as shown in FIG. 8. However, the subsequent steep reduction in soil Ni concentrations between spring (~ 5 m) and mid-summer (~7 m) is evidence for the uptake of soil Ni and depletion of the soil Ni pool by the hyperaccumulator plants at a time of increasing primary productivity as shown in FIG. 8. This data is evidence of the synergy between the two processes because depletion of the soil nickel pool by hyperaccumulator plants can be offset through the weathering of additional nickel bearing-minerals (e.g., serpentinite) introduced to the soil, resulting in carbon negative nickel recovery. \|Statistical analyses \|[0138] Statistical analysis was also performed to determine the significance of the relationships between rock application, plant nickel uptake, and (potential) carbon capture rates. Statistical analysis of the soil data was performed using a linear mixed model with fixed model Treatment * Time and random model of Block/Plot. Where appropriate, variables were first transformed to ensure homogeneity of variance. F statistics were obtained using the Kenward-Roger approximation. Statistical analysis of the plant data was performed using a linear model accounting for differences between blocks. A third order polynomial was fitted over application rate with highest order terms successively dropped if found to be non- significant. \|[0139] Regarding soil pH, statistically significant differences were observed both between treatments (F4, 12=21.54, p < 0.0001) and over time (F3, 45=7.18, p=0.0005). Predicted means and standard errors for each significant main effect is shown in FIGS. 9 and 10. For Soil EC, statistically significant differences were observed both between treatments (F4, 12=3.28, p = 0.049 - a marginal effect) and over time (F3, 45=8.59, p=0.0001). Predicted means and standard errors for each significant main effect are shown FIGS. 11 and 12. For ammonium acetate (AA) extractable nickel, statistically significant differences were observed both between treatments (F4, 12=5.66, p = 0.008) and over time (F3, 45=10.03, p<0.0001). Predicted means and standard errors for each significant main effect is shown in FIGS. 13 and 14. For ammonium acetate extractable magnesium, a statistically significant interaction effect was found between treatment and sampling date (F12,45=2.27, p=0.02). Overall, the largest effect is attributed to differences over time (F3, 45=6.81, p=0.007). Predicted means and standard errors are shown in FIG. 15. A multivariate correlation figures between all soil data can be seen in FIG. 16. \|[0140] The above preliminary data was collected over the first 8 months of the field trial experiment. Additional data will be gathered until 12 months after the start of the field trial experiment to further elucidate the relationship between the application rate of the weatherable rock and the accumulation of metal by the hyperaccumulator plant, the soil pH, the soil electrical conductivity, the weatherable rock-derivable cations in the soils and plants, and the heavy metals in the soils and the plants, as well as determining the weathering rate of the weatherable rock, the amount of nickel ore extractable from the plants, and quantifying the amount of carbon dioxide sequestered. \|Example 3: Field-scale enhanced rock weathering experiment with two controls\|[0141] In this example, a field- scale trial is employed to further investigate the synergistic combination of nickel phytomining and enhanced weathering. A scale diagram of the randomized complete block design used in the trial is shown in FIG. 17. The trial uses an approximately level 112 m x 208 m field site that is divided into four blocks of equivalent area, each measuring 56 m x 104 m, with every block subdivided into 10 randomly-assigned 12 m x 18 m plots representing the ten treatments as shown in FIG. 17. The amount of rock treatment added to each plot as measured in tonnes of serpentinite rock per hectare is shown in FIG. 17. Neither rock nor hyper- accumulator plants are added to the plots marked with ‘XX’ in FIG. 17. These plots are designed to simulate native soil conditions. The plots are segregated by an 8 m margin of untreated land. \|[0142] Two control treatments are included in this study: a rock-free control (i.e. 0 tonnes of rock added per hectare) where hyperaccumulator plants are grown, and a second control where no plants, rock amendments, or management practices are employed, as denoted by ‘XX’ in FIG. 5. The rock-free control is used to assess the effect of different rock applications on nickel uptake efficiency and carbon capture. The experiments with no plants, rock amendments, or management practices control serves a baseline (the native soil’s background conditions). \|Soil sample collection and measurements \|[0143] Following a W-shaped sampling pattern, multiple baseline soil samples are collected and aggregated from each of the forty plots at three discrete depths (0-0.3, 0.3-0.6 and 0.6-0.9 m) using a steel auger. These initial soil samples are separately homogenized, passed through a 2-mm mesh size sieve, and air-dried. Soils are then tested for pH (in H2O and IM KC1) and electrical conductivity (in H2O); inorganic/organic carbon and nitrogen %; plant-available nitrogen, phosphorus and potassium; soil texture (sand/silt/clay %), bulk density and water holding capacity; cation exchange capacity and exchangeable acidity; major oxide and soil mineralogy %; and, total and plant-available Ca, Mg, K, Na, Fe, Cd, Co, Cr, Cu, Mn, Ni, Pb, and Zn. Further soil samples are taken at bi -monthly intervals and tested to determine changes in fundamental soil parameters (pH, electrical conductivity, organic/inorganic carbon) and the concentration of exchangeable (plant- available) metals. These data are critical for monitoring changes in nickel availability and carbon dioxide capture rates in the plots. \|Plant sample collection and measurements \|[0144] Approximately 1-year after the start of the field trial, shoot tissues are harvested from all plots, and the shoot tissues are dried and weighed to quantify crop performance. In addition, plant materials are powdered, digested, and tested to determine metal content and analyze the correlation between rock application rate and nickel uptake efficiency. Total plant calcium, magnesium, potassium, and sodium values are added to the respective values from the soil analyses of exchangeable elements, which together enable the quantification of rock weathering and carbon capture rates. \|Aqueous sample collection and measurements \|[0145] Pore water samples are extracted from the soil using lysimeters installed in the plots. These aqueous samples are analyzed for changes in the following parameters: pH, electrical conductivity, and alkalinity; and dissolved cations (e.g. nickel, magnesium) and anions (e.g. chloride, nitrate). These data are essential for accurate monitoring of rock dissolution, nickel release, and carbon capture rates. Soil-atmosphere greenhouse gas sample collection and measurements \|[0146] Gaseous samples are collected during the trial using static chambers installed in the plots and are analyzed using gas analysis mass spectrometry to determine soil-atmosphere fluxes of major greenhouse gasses, such as carbon dioxide, methane, and nitrous oxide. This example seeks to determine the effects of the addition of alkaline rocks to the soil on overall emissions of potent non-CCh greenhouse gasses, and thus impact on climate change. These gas measurements are performed in serpentine soils, and also provide evidence that the soil amendments and agricultural management practices associated with the trial result in the conversion of existing soil organic carbon into atmospheric carbon dioxide. \|Example 4: Life Cycle Assessment at Kilotonne and Megatonne Scales Per Year\|[0147] A Life Cycle Assessment (LCA) was employed to ensure that the enhanced rock weathering/hyperaccumulator plant operation is sufficiently CO2 negative at the necessary scale. The aim was to model the net sequestration of 1 kilotonne and 1 megatonne of CO2 per year. The LCA was conducted using SimaPro software which draws data from various databases. The study adopted a cradle-to-gate approach, which includes all the major processes in the life cycle from the mining operation to the production of nickel ore, however the environmental impact of waste treatment was excluded from the LCA due to the ambiguity of its relevance. The two products of the operation are CO2 uptake (carbon dioxide removal through enhanced rock weathering) and the production of nickel ore through phytomining. The major processes within the established system boundaries include the mining, crushing, and milling of serpentine, the transportation of the serpentine rock to the site of placement, the fertilizer used, and harvesting, drying, and combustion of the hyperaccumulator plants. A unit area of land was used as the functional unit for the LCA to account for both the CO2 extraction and the nickel ore production. For example, per every m2 of area of serpentine soil used for the cultivation of A. Murale (or a similar hyperaccumulator plant), a certain amount of nickel will be produced and a certain amount of CO2 will be sequestered. This functional unit ensures that neither of the two products of the system (i.e. CO2 uptake and the production of nickel ore) are neglected from the LCA analysis and that their amounts are calculated independently of each other. \|[0148] The data used for the LCA was collected from several sources and the model was built on the basis of existing models. The data related to standard transportation, machinery, energy, and materials were kept as they were in the models, apart from several necessary adjustments to bring the model closer in line with the operation. For example, during the whole process, the electricity comes from the grid, where it is mostly produced using hydropower. This feature was reflected in the model. It is not required that hydropower be utilized in the process, though it will lower the net negative efficiency. A range of parameters, such as the weathering rate and serpentine content in soil, was introduced into the model. The information used to determine the parameter values was sourced from a combination of existing literature on similar experiments with hyperaccumulators and mineral weathering. The firm relied on rates of natural weathering processes which resulted in calculations that predict significant CO2 uptake and nickel production. \|[0149] The models for 1 kilotonne-scale production yearly can be seen in FIG. 18. The 1 megatonne-scale chart can be seen in FIGS. 19A and 19B. The main difference between the operations is the increased transport distance between the serpentine mining site and the farming sites in the megatonne- scale model as compared to thel kilotonne-scale model. Although not incorporated into the model, utilizing renewable energy for transportation of the rock between the mining site and farming sites would help ensure that the process remains CO2 negative even with long transportation distances. According to this LCA study, the operation can run at scale at an approximately 90% net efficiency in terms CO2 sequestration; additional details of the LCA study can be found in FIG. 20.	(WO2024/020548)\| METHODS FOR OBTAINING CARBON NEUTRAL OR CARBON NEGATIVE METALS FROM PLANTS, AND RELATED COMPOSITIONS \|CROSS-REFERENCE TO RELATED APPLICATIONS \|[0001] This application claims priority to and benefit of U.S. Provisional Application Serial No. 63/391,662, filed July 22, 2022, which is incorporated by reference in its entirety. \|FIELD \|[0002] The present disclosure relates generally to methods of extracting metals from rocks and sequestering carbon dioxide, and more specifically to methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. \|BACKGROUND \|[0003] Carbon dioxide is the dominant greenhouse gas released by human activities and the major contributor to global warming. Carbon sequestration is the process of capturing and storing atmospheric carbon dioxide. It is the only approach that humans can use to actively reduce the amount of carbon dioxide in the atmosphere. Currently, two main types of carbon sequestration are geologic carbon sequestration and biologic carbon sequestration. Current methods for sequestering carbon dioxide, such as underground sequestration, generally face problems related to economic viability, carbon dioxide leakage, and potential contamination of groundwater. Accordingly, there exists a need in the art for cost-effective methods to remove carbon dioxide from the atmosphere at a gigatonne scale while minimizing the negative impacts on the environment. \|BRIEF SUMMARY \|[0004] In some aspects, provided herein are methods and systems that combine enhanced weathering and phytomining to not only sequester carbon dioxide but also extract metals from surrounding soil. Enhanced weathering, which includes terrestrial enhanced weathering and oceanic enhanced weathering, is weathering accelerated by spreading finely ground silicate rock onto surfaces. This helps to accelerate chemical reactions between rocks, water and air. Phytomining refers to the use of hyperaccumulator plant species to concentrate metals from soils and subsequently processing the hyperaccumulator biomass to generate useful metal products. Hyperaccumulators are rare plants that draw up metal from the soil on which they grow, and accumulate high levels of metals in their biomass.\|[0005] In some embodiments, the metals may comprise nickel, cobalt, chromium or any combination thereof. In some embodiments, the methods and systems provided sequester carbon dioxide through a chemical weathering process that results in the release of Mg2+ ions. In some embodiments, the metals are phytomined from serpentinite. Serpentinite is a rock comprising one or more of the serpentine group minerals. Minerals in this group are rich in magnesium and iron. Serpentinite has been called serpentine or serpentine rock, particularly in older geographical texts and in wider cultural settings. In some embodiments, serpentinite is a rock comprising one or more of the serpentine group minerals. In some embodiments, serpentinite is a rock comprising one or more minerals having the chemical formula D3[Si2Os](OH)4, wherein D is selected from the group consisting of Mg, Fe, Ni, Mn, Al, and Zn. In some embodiments, serpentinite is a rock comprising one or more mineral selected from the group consisting of amesite, antigorite, berthierine, brindleyite, caryopilite, chrysotile, cronstedtite, fraipontite, guidottiite, kellyite, lizardite, nepouite, and pecoraite. \|[0006] In some embodiments, the methods and systems provided utilize plant species that are tolerant to soils having high metal contents. In some embodiments, the plants are tolerant of high pH soils. In some embodiments, the plants are tolerant of low nutrient soils. In some embodiments, the plants are hyperaccumulators of nickel. In some variations, provided is a method comprising transporting weatherable rock from a quarry, using mechanical activation to grind the weatherable rock to particles to increase reactive mineral surface area, dispersing the weatherable rock particles into the soil within a plot of land, planting nickel hyperaccumulating plants onto the plot of land to capture the nickel released from the weatherable rock during chemical weathering. In some embodiments, the presence of the nickel hyperaccumulating plants accelerates the chemical weathering of the weatherable rock. In some embodiments, the nickel hyperaccumulating plants may be harvested and further processed to yield a purified nickel composition. In some embodiments, the weatherable rock is ground to a particle size suitable to optimize both the rate of chemical weathering and the rate of nickel accumulation in the hyperaccumulating plant. In some embodiments, grinding the rock to particles comprises grinding the rock to a size of between about 1 pm and about 10 cm. In some variations of the foregoing, the weatherable rock comprises serpentine. In some variations of the foregoing, the weatherable rock comprises serpentinite. \|[0007] In some embodiments, the nickel may be nickel metal in oxidation state 0, or any suitable nickel salts and nickel complexes, such as Ni2+ salts. In some variations, the nickel is a Ni2+ salt or complex. In some embodiments, the nickel may be in an oxidation state of -1, 0, 1, 2, 3, or 4, or any combination thereof. \|[0008] In some variations, the weatherable rock may be obtained from the tailings, waste, or overburden from traditional nickel mines. In some embodiments, the weatherable rock comprises serpentine. In some embodiments, the nickel hyperaccumulating plants are directly irrigated. In some embodiments, the irrigation is accomplished using a continuous irrigation system. In some embodiments, the irrigation is accomplished using an automated irrigation system. \|[0009] In some variations, the methods and systems employ hyperaccumulator plants that are capable of growing in high and even pure levels of serpentine and that are be able to survive and accelerate the weathering rate of the serpentine minerals, especially when fertilized and irrigated. \|[0010] In one aspect, provided is a method for obtaining nickel metal, comprising mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium, and at least 0.1% by weight of nickel to provide a particulate weatherable rock composition, combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil, harvesting the nickel hyperaccumulator plant, and processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel. \|[0011] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash comprising at least 5% nickel by weight, and refining the nickel-enriched ash composition to provide a substantially pure nickel. \|[0012] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises heat treating the harvested nickel hyperaccumulator plant to provide a nickel- enriched ash comprising at least 5% nickel by weight, and refining the nickel-enriched ash composition to provide a substantially pure nickel. \|[0013] In certain embodiments, Mg2+ is leached from the weatherable rock-enriched soil at a rate faster than the observed rate of stationary ultramafic minerals, or minerals without plants growing in them. In certain embodiments, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the nickel hyperaccumulator plant is growing. \|[0014] In other variations, the method may be employed for obtaining one or more metals, including nickel, cobalt, chromium or any combination thereof. In variations where a plurality of metals are obtained, multiple hyperaccumulator plants suitable for harvesting the metals are employed in the process. For example, in some variations of the methods, a nickel hyperaccumulator plant and a cobalt hyperaccumulator plant are used in the weatherable rock-enriched soil to harvest a combination of nickel and cobalt. \|[0015] In some embodiments, at least 10 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. \|[0016] In some embodiments, the weatherable rock comprises ultramafic rock. In some embodiments, the weatherable rock comprises mafic rock. In some embodiments, the weatherable rock comprises less than about 55% silica by weight. In some embodiments, the weatherable rock comprises less than about 45% silica by weight. In some embodiments, the weatherable rock comprises between about 45% and about 55% silica by weight. In some embodiments the weatherable rock comprises one or more minerals selected from the serpentine group. In some embodiments, the weatherable rock comprises olivine. In some embodiments, the weatherable rock comprises serpentinite. In some embodiments, the weatherable rock comprises gabbro or basalt, or a combination. In some embodiments, the weatherable rock comprises a combination of mafic rocks or minerals. \|[0017] In some embodiments, the method comprises mining the weatherable rock. In some embodiments, the method comprises transporting the mined weatherable rock from a mining location to a grinding location. In some embodiments, the method comprises mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock. \|[0018] In some embodiments, the particulate weatherable rock composition has a particle size between 1 pm and 10 cm. In some embodiments, the weatherable rock-enriched soil comprises between 10% and 100% particulate weatherable rock composition by weight. \|[0019] In some embodiments, the nickel hyperaccumulator plant is a plant belonging to the genus Odontarrhena. In some embodiments, the nickel hyperaccumulator plant is grown inside of a greenhouse. In some embodiments, the nickel hyperaccumulator plant is grown under polyethylene film (e.g., a polytunnel). \|[0020] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil. In some embodiments, the pH of the weatherable rock-enriched soil is at least 7. In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises intermittently irrigating the weatherable rock-enriched soil. \|[0021] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises fertilizing the plant. In some embodiments, nitrogen, phosphorus, and potassium (NPK) fertilizers are used to fertilize the plant. In some embodiments, calcium is added to the soil. In some embodiments, boron is used to stimulate flowering in the plant. In some embodiments, soil analysis is used to determine which nutrients are lacking in the soil. In some such embodiments, fertilizer is used to provide the plant with one or more of the nutrients that are determined as lacking in the soil. In some embodiments, exogenous additives are used to increase the available levels of metals in the soil. In some embodiments the exogenous additive comprises citric acid. In some embodiments, potassium is added to the soil. In some embodiments, sulphur-containing compounds are added to the soil. \|[0022] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprises drying the nickel hyperaccumulator plant to provide a dried biomass composition, crushing the dried biomass composition to provide a crushed biomass composition, and burning the crushed biomass composition to provide a nickel-enriched ash composition. \|[0023] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises directly leaching the harvested nickel hyperaccumulator plant using sulfuric acid to provide an acid leachate; purifying the acid leachate using column chromatography to provide a Ni-enriched acid leachate; and further processing the Ni-enhanced acid leachate to provide a substantially pure nickel. \|[0024] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises leaching the nickel-enriched ash composition to provide a leachate; recovering nickel from the leachate using solvent extraction or an ion exchange resin to obtain a recovered nickel composition; and purifying the recovered nickel composition using electrowinning to obtain a substantially pure nickel. \|[0025] It should be understood that, in other variations, the embodiments of the method described above for harvesting nickel may be modified to harvest one or more other metals, such as cobalt and chromium, or any combinations of such metals. \|[0026] In some embodiments, refining the nickel-enriched ash composition comprises: acid leaching the nickel-enriched ash composition to provide an acid leachate; neutralizing the acid leachate with Ca(OH)2 to provide a first treated leachate; adding NaF to the neutralized leachate to provide a second treated leachate; adding ammonium sulfate to the second treated leachate to provide a third treated leachate; drying the third treated leachate to provide ammonium Ni sulfate hexahydrate (ANSH); and processing the ANSH to obtain a substantially pure nickel. \|[0027] In some embodiments, the method further comprises quantifying the amount of carbon dioxide that is released or sequestered in one or more steps of the method. \|[0028] In another aspect, provided is nickel metal prepared according to any of the foregoing methods. \|[0029] In another aspect, provided is a processed nickel composition comprising substantially pure nickel, and one or more of the following: (i) precipitated gypsum, (ii) one or more low weight carboxylic acids, (iii) one or more Ni-containing compounds selected from the group consisting of NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, nickel oxalate, and nickel sulfate, or (v) one or more carbonates selected from the group consisting of K2CO3, CaCO3, K2Ca(CO3)2. \|[0030] In another aspect, provided is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: (i) one or more elements selected from the group consisting of Ca, Fe, K, Mg, P, C, H, N, and O, (ii) one or more carbonates selected from the group consisting of K2CO3, CaCO3, K2Ca(CO3)2, (iii) plant cells, (iv) hydroxyapatite or oxyhydroxyapatite, or (v) one or more oxides selected from the group consisting of NiO, CaO, MgO, and MgNiO2.\|[0031] In yet other aspects, provided is a metal-enriched ash obtained by any of the methods described herein. In some variations, the metal is nickel, cobalt, or chromium, or a combination thereof. \|DESCRIPTION OF THE FIGURES \|[0032] The present application can be understood by reference to the following description taken in conjunction with the accompanying figures. \|[0033] FIG. 1 depicts an exemplary process for obtaining metal using weatherable rock and phytomining. \|[0034] FIG. 2 depicts the different growing conditions employed in the assessment of weathering rates for different soil and plant configurations. \|[0035] FIG. 3 depicts the total amount of magnesium leached under each of the conditions of FIG. 2 over the course of 4 months. \|[0036] FIGS. 4 depicts a diagram of an exemplary field- scale randomized complete block design used to investigate the synergistic combination of nickel phytomining and enhanced weathering. \|[0037] FIG. 5 depicts the pH analysis of topsoils for five application rates approximately eight months after crushed serpentinite rock was applied. \|[0038] FIG. 6 depicts the electrical conductivity analysis of topsoils for five application rates approximately eight months after crushed serpentinite rock was applied. \|[0039] FIG. 7 depicts the amount of nickel in the shoot tissues of hyperaccumulator plants grown on soils treated with eight different application rates of serpentinite rock. \|[0040] FIG. 8 depicts the results from a time-series analysis of topsoil Ni concentrations for five application rates using a Mehlich 1 reagent. \|[0041] FIGS. 9 and 10 depicts the results of statistical analysis of the pH of the soil with respect to application rate and sampling time, respectively. \|[0042] FIGS. 11 and 12 depicts the results of statistical analysis of the electrical conductivity of the soil with respect to application rate and sampling time, respectively.\|[0043] FIGS. 13 and 14 depicts the results of statistical analysis of the ammonium acetate extractable nickel content of the soil with respect to application rate and sampling time, respectively. \|[0044] FIG. 15 depicts the results of statistical analysis of the ammonium acetate extractable magnesium content of the with respect to application rate and sampling time. \|[0045] FIG. 16 depicts a multivariate correlation of the statistical analysis of the soil data. \|[0046] FIG. 17 depicts a diagram of another exemplary field-scale randomized complete block design used to investigate the synergistic combination of nickel phytomining and enhanced weathering. \|[0047] FIG. 18 depicts the life cycle assessment model for an exemplary 1 kilotonne-scale production. \|[0048] FIGS. 19A and 19B depict the life cycle assessment model for an exemplary 1 megatonne-scale production. \|[0049] FIG. 20 depicts additional data used in the life cycle assessment of an exemplary process. \|DETAILED DESCRIPTION \|[0050] The following description sets forth exemplary compositions, methods, systems, parameters and the like. It should be recognized, however, that such description is not intended as a limitation on the scope of the present disclosure but is instead provided as a description of exemplary embodiments. \|[0051] In one aspect, provided herein is a method of sequestering carbon dioxide comprising providing a weatherable rock comprising one or more metals, subjecting the weatherable rock to conditions sufficient to cause the rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the one or more metals, and wherein the alkalinity facilitates the sequestration of carbon dioxide through the conversion of carbon dioxide to bicarbonate or carbonate, and extracting and processing the released metals to provide a metal-enriched composition. In some embodiments, the conditions cited above comprise growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock. In some embodiments, the conditions comprise growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock and continuously irrigating the one or more metal hyperaccumulator plants using a drip irrigation system. In some embodiments, the extracting and processing the released one or more metals comprises growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock, wherein the one or more metal hyperaccumulator plants accumulate the released one or more metals. In some embodiments the extracting and processing the released one or more metals further comprises processing the metal hyperaccumulator biomass using any suitable technique known in the art to prepare a metal-enriched composition. In some embodiments, the one or more metals comprise a heavy metal. In some embodiments, the one or more metals comprise a toxic metal. In some embodiments, the one or more metals comprise a metal selected from the group consisting of Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the one or more metals comprise cobalt. In some embodiments, the one or more metals comprise chromium. In some embodiments, the one or more metals comprise nickel. In some embodiment the one or more metals comprise any metal that can be hyperaccumulated by a hyperaccumulator plant. In some embodiments, providing the weatherable rock comprises mining the weatherable rock. In some embodiments, providing the weatherable rock further comprises mechanically processing the weatherable rock to reduce the particle size of the weatherable rock to between about 1 pm and about 10 cm. In some embodiments, providing the weatherable rock further comprises admixing the weatherable rock with one or more additional growing media including, for example, soil. \|[0052] In one aspect, provided herein is a method of sequestering carbon dioxide comprising providing a weatherable rock comprising a metal, subjecting the weatherable rock to conditions sufficient to cause the rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide through the conversion of carbon dioxide to bicarbonate or carbonate, and extracting and processing the released metal to provide a metal-enriched composition. In some embodiments, the conditions cited above comprise growing a metal hyperaccumulator plant in a medium comprising the weatherable rock. In some embodiments, the conditions comprise growing a metal hyperaccumulator plant in a medium comprising the weatherable rock and continuously irrigating the metal hyperaccumulator plant using a drip irrigation system. In some embodiments, the extracting and processing the released metal comprises growing a metal hyperaccumulator plant in a medium comprising the weatherable rock, wherein the metal hyperaccumulator plant accumulates the released metal. In some embodiments the extracting and processing the released metal further comprises processing the metal hyperaccumulator biomass using any suitable technique known in the art to prepare a metal-enriched composition. In some embodiments, the metal is a heavy metal. In some embodiments, the metal is a toxic metal. In some embodiments, the metal is selected from the group consisting of Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the metal comprises cobalt. In some embodiments, the metal comprises chromium. In some embodiments, the metal comprises nickel. In some embodiment the metal is any metal that can be hyperaccumulated by a hyperaccumulator plant. \|[0053] In some embodiments, the weatherable rock comprises a magnesium-bearing silicate mineral. In certain embodiments, the magnesium-bearing silicate mineral is in the olivine mineral group. In certain embodiments, the magnesium-bearing silicate mineral is in the serpentinite mineral group. In other variations, any combination of suitable weatherable rocks described herein may be used. \|[0054] In some embodiments, providing the weatherable rock comprises mining the weatherable rock. In some embodiments, providing the weatherable rock further comprises mechanically processing the weatherable rock to reduce the particle size of the weatherable rock to between about 1 pm and about 10 cm. In some embodiments, providing the weatherable rock further comprises admixing the weatherable rock with one or more additional growing media including, for example, soil. \|[0055] In another aspect, provided herein is a method that utilizes plants that are not only tolerant to serpentine, but that evolved especially to live in high alkalinity (e.g., high pH) soils, composed of high percentages of low nutrient and metal heavy soils. These plants that typically take up nickel as a means of protection can be utilized to produce commercial yields of nickel. In certain aspects, provided is a method to bring fresh serpentine-containing rock from nearby quarries, utilizing mechanical activation to grind them to particles, for example micron-sized particles, to increase the reactive surface area, then transported to fields where nickel hyperaccumulating plants have been planted to capture the nickel release from the soil, and also accelerate the release of magnesium ions from the crystal lattice of the serpentine in order to increase the amount of carbon sequestered when those ions run off to the ocean. The methods provided herein overcome the previous blockers that prevented the deployment of terrestrial enhanced weathering for the purposes of carbon removal, and by increasing the revenue streams available to the process are able to make direct and intentional phytomining possible. The methods provided make phytomining a primary mining technique. In some variations, the methods can also use tailings, waste, or overburden from traditional nickel mines. In certain variations, the methods involve actively grinding minerals to below a certain size in order to specifically increase the reactive surface area. Further, in some variations, direct irrigation can be utilized to both enhance the weathering rate, and increase the plant growth, the plant then releases acids that further break down the rocks, releasing magnesium that leads to carbon removal and drawing nickel into the plants, preventing its release into the environment. \|[0056] In some variations of the foregoing, the chemical weathering process results in the formation of new soil minerals. In certain variations of the foregoing, the chemical weathering process results in fully weathered rock. In some embodiments, the weathering process results in fully weathered rock within about 20 years; or between 1 year and 20 years; or within about 1 year, about 2 years, about 3 years, about 4 years, about 5 years, about 6 years, about 7 years, about 8 years, about 9 years, about 10 years, about 11 years, about 12 years, about 13 years, about 14 years, about 15 years, about 16 years, about 17 years, about 18 years, about 19 years, or about 20 years. \|[0057] With reference to FIG. 1, depicted is an exemplary process 100 for obtaining metal using weatherable rock and phytomining. Step 102 involves mechanically grinding a weatherable rock to provide a particulate weatherable rock composition. In step 104, the particulate weatherable rock composition is combined with a soil to provide a weatherable rock-enriched soil. In step 106, a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil is grown. Then, in step 108, the metal hyperaccumulator plant is harvested. In step 110, the harvested metal hyperaccumulator plant is processed using any suitable techniques or methods known in the art to provide a substantially pure metal. In some variations of the process, step 110 may be optional. For example, in certain variations, the process described herein does not require harvesting of the metal from the plant to obtain a substantially pure metal. In other variations, the process further includes harvesting of the metal from the plant to obtain a substantially pure metal.\|[0058] Thus, in some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising magnesium, and a metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil; harvesting the metal hyperaccumulator plant; and processing the harvested metal hyperaccumulator plant to provide a substantially pure metal. In some embodiments, processing the harvested metal hyperaccumulator plant comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide a substantially pure metal by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide a substantially pure metal may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 20% by weight of magnesium and 0.1% by weight of the metal. In some embodiments, the metal-enriched ash comprises at least 5% of the metal by weight. \|[0059] In some embodiments, provided is a method for preparing one or more metals comprising mechanically grinding a weatherable rock comprising magnesium, and one or more metals to provide a particulate weatherable rock composition; either combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil or using the particulate weatherable rock composition directly as a weatherable rock- enriched soil without combining it with any additional media; growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil, wherein each of the one or more plants is a hyperaccumulator of at least one of the one or more metals; harvesting the one or more metal hyperaccumulator plants; and processing the one or more harvested metal hyperaccumulator plants to provide one or more substantially pure metals. In some embodiments, processing the one or more harvested metal hyperaccumulator plants comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide one or more substantially pure metals by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide one or more substantially pure metals may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 20% by weight of magnesium and 0.1% by weight of each of the one or more metals. In some embodiments, the metal-enriched ash comprises at least 5% of each of the one or more metals by weight.\|[0060] In some embodiments, provided is a method for obtaining one or more substantially pure metals comprising mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium and at least 0.1% by weight of each of the one or more metals to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil, wherein each of the one or more plants is a hyperaccumulator of at least one of the one or more metals; harvesting the one or more metal hyperaccumulator plants; and processing the one or more harvested metal hyperaccumulator plants to provide one or more substantially pure metals. \|[0061] In some variations, substantially pure metal refers to a metal that is at least 90%, at least 95%, at least 96%, at least 97%, at least 98%, at least 99%, at least 99.9%, at least 99.99%. at least 99.999%, or at least 99.9999% pure by weight. \|[0062] In some embodiments, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the metal hyperaccumulator plant is growing. In some embodiments, about 10% of the Mg by weight is weathered per year. In some embodiments, about 90% of the Mg by weight is weathered per month. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated over a period of about 20 years. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated over a period of less than about 20 years. In any of the foregoing embodiments, the weight of Mg2+ refers to the weight of the magnesium component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts that the Mg2+ is a part of. \|[0063] In some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising calcium and a metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil; harvesting the metal hyperaccumulator plant; and processing the harvested metal hyperaccumulator plant to provide a substantially pure metal. In some embodiments, processing the harvested metal hyperaccumulator plant comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide a substantially pure metal by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide a substantially pure metal may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 10% by weight of calcium and at least 0.1% by weight of the metal. In some embodiments, the metal-enriched ash comprises at least 5% of the metal by weight. \|[0064] In some embodiments, Ca2+ is leached at a rate of at least 1% by weight of the total Ca2+ in the weatherable rock per year from the weatherable rock-enriched soil while the metal hyperaccumulator plant is growing. In some embodiments, about 10% of the Ca by weight is weathered per year. In some embodiments, about 90% of the Ca by weight is weathered per month. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated over a period of about 20 years. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated over a period of less than about 20 years. In any of the foregoing embodiments, the weight of Ca2+ refers to the weight of the calcium component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts that the Ca2+ is a part of. \|[0065] In some embodiments, the rate at which Mg2+ is leached is measured by measuring the concentration of the Mg2+ in the water used to irrigate the hyperaccumulator plant. In some embodiments, the rate at which Ca2+ is leached is measured by measuring the concentration of Ca2+ in the water used to irrigate the hyperaccumulator plant. \|[0066] In some variations of the foregoing, the weatherable rock comprises between 0.01% and 20% of the metal by weight. In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of the metal by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of the metal. \|[0067] In some embodiments, the metal comprises Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the metal comprises a rare earth metal. In some embodiments, the metal comprises nickel. In some embodiments, the metal comprises cobalt. In some embodiments, the metal comprises chromium. In some embodiments, the metal is a metal that can be hyperaccumulated by a hyperaccumulator plant. In some embodiments, the metal is a metal found in a weatherable rock. In some embodiments, the metal is a metal found in a weatherable rock that can be hyperaccumulated by a hyperaccumulator plant. \|[0068] In some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising magnesium and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; liberating nickel from the weatherable rock by subjecting the weatherable rock-enriched soil to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein acid is not added to the weatherable rock- enriched soil; growing a plant that is a hyperaccumulator of nickel in the weatherable rock- enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide substantially pure nickel. \|[0069] In some embodiments, the amount of carbon dioxide emitted from the weathering of the weatherable rock is less than amount of carbon dioxide sequestered from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide emitted from the weathering of the weatherable rock, harvesting the nickel hyperaccumulator plant, and processing the harvested nickel hyperaccumulator plant is less than amount of carbon dioxide sequestered from the weathering of the weatherable rock. \|[0070] In some embodiments, provided is a method for preparing nickel metal comprising mechanically grinding a weatherable rock comprising magnesium, and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel. In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash and refining the nickel-enriched composition to provide a substantially pure nickel by weight. In some embodiments, processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 10% by weight of magnesium and at least 0.1% by weight of nickel. In some embodiments, the nickel-enriched ash comprises at least 5% nickel by weight. \|[0071] In some variations of the foregoing, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the nickel hyperaccumulator plant is growing. \|[0072] In some variations of the foregoing, the weatherable rock comprises between 5% and 60% Mg by weight. In some embodiments, the weatherable rock comprises between 25% and 50% Mg by weight. In some embodiments, the weatherable rock comprises about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, or about 70% Mg by weight. \|[0073] In some variations of the foregoing, the weatherable rock comprises between 5% and 60% Ca by weight. In some embodiments, the weatherable rock comprises between 25% and 50% Ca by weight. In some embodiments, the weatherable rock comprises about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, or about 70% Ca by weight. \|[0074] In some variations of the foregoing, the weatherable rock comprises between 0.01% and 20% of nickel by weight. In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of nickel by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of nickel. \|[0075] In some variations of the foregoing, the weatherable rock comprises nickel and Mg. In some embodiments, the weatherable rock comprises between 0.01% and 25% of nickel by weight and between 5% and 60% of Mg by weight. In some embodiments, the weatherable rock comprises between 0.01% and 25% of nickel by weight and between 25% and 50% of Mg by weight. \|[0076] In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of nickel by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of nickel. \|[0077] In some variations of the foregoing, the nickel-enriched ash composition comprises between 1% and 99.8% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 1% and 35% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 1% and 30% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 30% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 20% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 15% nickel by weight. In some embodiments, the nickel- enriched ash composition comprises about 0.1%, about 0.5%, about 1%, about 1.5%, about 2%, about 2.5%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, or about 40% nickel by weight. \|[0078] In some variations of the foregoing, refining the nickel-enriched composition provides a nickel that is at least 15%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 98%, at least 99%, at least 99.9%, at least 99.9%, at least 99.99%, at least 99.999%, or at least 99.9999% pure by weight. In some embodiments, refining the nickel-enriched composition provides a nickel that is between 15% and 100% pure by weight. \|[0079] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprises drying the nickel hyperaccumulator plant to provide a dried biomass composition, crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a nickel-enriched ash composition. In some embodiments, the ashing is performed at a temperature of about 500 °C. \|[0080] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises directly leaching the harvested nickel hyperaccumulator plant to provide a leachate; purifying the leachate to provide a Ni-enriched leachate; and further processing the Ni-enhanced leachate to provide a substantially pure nickel. In some embodiments, the direct leaching is performed using a hydrothermal process. In some embodiments, the direct leaching is performed in acid. In some embodiments, the acid is sulfuric acid. In some embodiments, the acid is hydrochloric acid. In some embodiments purifying the leachate comprises purifying the leachate using column chromatography. In some embodiments purifying the leachate comprises purifying the leachate using solvent extraction. In some embodiments purifying the leachate comprises purifying the leachate using ion exchange chromatography. In some embodiments, further processing the Ni-enhanced leachate comprises electrowinning the nickel. \|[0081] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash, leaching the nickel-enriched ash composition to provide a leachate, treating the leachate to provide ammonium Ni sulfate hexahydrate (ANSH), and processing the ANSH to obtain a substantially pure nickel. In some embodiments, the leaching is performed in acid. In some embodiments treating the leachate comprises neutralizing the leachate using a base to provide a first treated leachate, adding a fluoride source to the first treated leachate to provide a second treated leachate, adding ammonium sulfate to the second treated leachate to provide a third treated leachate, and drying the third treated leachate to provide ANSH. In some embodiments, the base is Ca(OH)2. In some embodiments, the fluoride source is NaF. In some embodiments, treating the leachate comprises purifying the ANSH via recrystallization. \|[0082] In some embodiments, provided is a method for preparing nickel catalysts comprising mechanically grinding a weatherable rock comprising magnesium, and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide nickel catalysts. In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash, leaching the nickel-enriched ash to provide a leachate, and further processing the leachate to provide nickel catalysts. In some embodiments, the ashing is performed at a temperature of 500 °C. In some embodiments, the leaching is performed in acid. In some embodiments, the acid is hydrochloric acid. In some embodiments, further processing the leachate to provide nickel catalysts comprises dispersing the leachate onto montromorillonite K10. In some embodiments, the weatherable rock comprises at least 10% by weight of magnesium and at least 0.1% by weight of nickel.\|[0083] In some embodiments, the amount of carbon dioxide sequestered is on the tonne scale for every tonne of nickel metal that is produced. In some embodiments, at least 1 tonne, at least 5 tonnes, at least 10 tonnes, at least 20 tonnes, at least 30 tonnes, or at least 40 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. In some embodiments, between 1 tonne and 100 tonnes, or between 10 tonnes and 100 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. In some embodiments, between 100 tonnes and 500 tonnes, or between 300 tonnes and 500 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. \|[0084] In some embodiments, the weatherable rock comprises an ultramafic rock. In some embodiments, the weatherable rock comprises serpentine. In some embodiments, the weatherable rock comprises serpentinite. In some embodiments, the weatherable rock comprises olivine. In some embodiments, the weatherable rock contains less than 1% by weight of nickel. In some embodiments, the weatherable rock contains a metal that can be hyperaccumulated by a hyperaccumulator plant. \|[0085] In some embodiments, the method further comprises mining the weatherable rock. In other embodiments, the method further comprises transporting the mined weatherable rock from a mining location to a grinding location. \|[0086] In some embodiments, mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock. In some embodiments, the energy used to mechanically grind the rock comes from renewable sources. \|[0087] In some embodiments, the particulate weatherable rock composition has an average particle size between about 1 pm and about 10 mm, between about 1 pm and about 10 cm, between about 1 pm and about 20 cm, between about 1 pm to about 5 mm, between about 1 pm to about 3 mm, or between about 100 pm to about 3 mm. \|[0088] In some embodiments, the weatherable rock-enriched soil comprises between 10% and 100%, between 70% and 100%, between 70% and 90%, between 70% and 80%, or between 80% and 90% particulate weatherable rock composition by weight. In certain embodiments, the weatherable rock-enriched soil comprises about 30%, about 40%, about 50%, about 60%, about 70%, about 80%, about 90%, or about 100% particulate weatherable rock composition by weight.\|[0089] In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of silicate rocks. In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of serpentinite rocks. In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of olivine rocks. In some embodiments, natural weathering of serpentinite rocks results in weatherable rock-enriched soil with high nickel concentrations. \|[0090] In some embodiments, the nickel hyperaccumulator plant is a plant belonging to the genus Odontarrhena. In some embodiments the plant belongs to the genus Alyssum. In some embodiments the plant belongs to the family Brassicacaea. In some embodiments the plant belongs to the genus Bornmuellera. In some embodiments the plant belongs to the genus Thlaspi. In some embodiments, the plant is Alyssum Murale. In some embodiments, the plant is of the genus Odontarrhena. In some embodiments, the plant is Odontarrhena chalcidica. In some embodiments, the plant is Odontarrhena decipiens. In some embodiments, the plant is Berkheya coddii. In some embodiments, the plant is B. emarginata. In some embodiments, the plant is Stackhousia tryonii. In some embodiments, the plant is Phyllanthus balgooyi. In some embodiments, the plant is Rinorea bengalensis. In some embodiments, the plant may be a tree, bush, or vine. In some embodiments, the plant is a genetically modified plant. In some embodiments, the plant is any plant capable of hyperaccumulating a metal found in a weatherable rock. In some embodiments, the plant is any plant capable of hyperaccumulating nickel. In some embodiments, the plant is any hyperaccumulator plant species of the class known as a hypernickelophores, containing more than 1,000 pg Ni g 1. \|[0091] In some embodiments, the nickel hyperaccumulator plant is grown inside of a greenhouse. In some embodiments, the nickel hyperaccumulator plant is grown inside of a vertical farm. In some embodiments, the nickel hyperaccumulator plant is grown hydroponically. In some embodiments, the nickel hyperaccumulator plant is grown under a polyethylene film (e.g., a polytunnel). \|[0092] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the weathering rate of the weatherable rock. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the efficiency of nickel uptake by the plant. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the weathering rate of the weatherable rock and the efficiency of nickel uptake by the plant. \|[0093] In some embodiments, the environmental conditions of the weatherable rock- enriched soil are controlled to cause the weatherable rock to undergo a chemical weather process at an accelerated rate relative to natural chemical weathering environmental conditions. In some embodiments, the conditions cited above comprise growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil. In some embodiments, the conditions comprise growing one or more metal hyperaccumulator plants in a weatherable rock-enriched soil and continuously irrigating the one or more metal hyperaccumulator plants using a drip irrigation system. In some embodiments, the temperature, pH, irrigation, or bioactivity of the weatherable rock-enriched is controlled. \|[0094] In some embodiments, the rate of weathering of the weatherable rock is between about 0% and about 40% by mass of the weatherable rock between about 12 months and about 72 months from the date of combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil and planting the hyperaccumulator plant in the weatherable rock-enriched soil. Any suitable methods known in the art may be used to determine the rate of weathering of the weatherable rock. For example, in one variation, the foregoing rates of weathering may be calculated using the Arrhenius equation. \|[0095] In some embodiments, the weathering rate is calculated by measuring the accumulation of rock-derived cations (e.g., Ca, Mg, Na, and K) in plant, soil, and/or aqueous effluent associated within a certain plot of land and subtracting the baseline amount of the corresponding cation measured in a corresponding control plot. For example, the net accumulation of Ca-cations due to mineral dissolution of weatherable rock can be calculated by subtracting the amount of Ca-cations measured in a control plot from the total amount of Ca-cations calculated by totaling the amount of Ca-cations in the water and/or effluent, the Ca-cations in plant tissues, and Ca-cations in the soil cation exchange pool. The amount of Ca-cations attributable to the weathering of weatherable rock can then be converted into spatially-averaged cation weathering rates (per unit of land area) or rates related to mineral surface area. In some embodiments, the weatherable rock is calculated in the number of moles of calcium, magnesium, sodium, and/or potassium released from the weatherable rock material into the soil per hectare of treated land per annum.\|[0096] In some embodiments, the weathering rate of the weatherable rock increases when the average particle size of the weatherable rock decreases. \|[0097] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to increase the weathering rate of the weatherable rock. In some embodiments, the environmental parameter that is optimized to increase the weathering rate of the weatherable rock is temperature. In some embodiments, the temperature of the surrounding air (e.g., climate) is increased to increase the weathering rate of the weatherable rock. In some embodiments, the temperature of the topsoil (e.g., where the weatherable rock is admixed into the soil) is increased to increase the weathering rate of the weatherable rock. In some embodiments, the amount of irrigation of the soil admixed with the weatherable rock is increased to increase the weathering rate of the weatherable rock. In some embodiments, the pH of the soil admixed with the weatherable rock is increased to decrease the weathering rate of the weatherable rock. In some embodiments, the pH of the soil admixed with the weatherable rock is decreased to increase the weathering rate of the weatherable rock. \|[0098] In some embodiments, the weathering rate of the weatherable rock is increased by increasing the amount of biological activity of the soil admixed with the weatherable rock. In certain embodiments, the increased biological activity of the soil is measured by the amount of carbon dioxide produced by the microbes per a given amount of the soil. In certain embodiments, the increased biological activity of the soil is measured by the amount of nitrogen-cycling and secretion of organic acids by plant roots and mycorrhizal fungi present in the soil. \|[0099] In some embodiments, increasing the concentration of Mg2+ ions in the soil admixed with the weatherable rock increases the weathering rate of the weatherable rock. In some embodiments, increasing the concentration of Ca2+ ions in the soil admixed with the weatherable rock increases the weathering rate of the weatherable rock. In certain variations, higher soil Ca and Mg content may decrease the weathering rate of rock material added to the soil, because chemical conditions in the groundwater may approach saturation for certain Ca- (and Mg-) bearing minerals. \|[0100] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the accumulation of nickel by the plant. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the growth rate of the plant. In some embodiments, the humidity, temperature, or lighting of the environment in which the nickel hyperaccumulator plant is grown are controlled. In some embodiments, the nickel hyperaccumulator plant is grown in an outdoor field. \|[0101] In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to maximize the accumulation of nickel by the hyperaccumulator plant. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is between about 5 tonnes and 300 tonnes. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is between about 10 tonnes and 50 tonnes. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is about 37 tonnes. \|[0102] In some embodiments, the amount of nickel accumulated by a nickel hyperaccumulator plant increases proportionally with the amount of weatherable rock mixed into the soil in which the plant is grown. In some embodiments, increasing the amount of weatherable rock mixed in the soil does not result in an increase in the amount of nickel accumulated by a hyperaccumulator plant growing in the soil. In certain embodiments, high amounts of weatherable rock mixed into the soil result in high alkaline (e.g., high pH) soils which can negatively impact the mobility of the one or more metals released from the weatherable rock during the weathering process. \|[0103] In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown and the environmental conditions under which the hyperaccumulator plant is grown are optimized to control the pH of the soil. In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to control the pH of the soil. In some embodiments, an increase in the pH of the soil decreases the mobility of the one or metals released by the weatherable rock mixed in the soil. In some embodiments, decreased mobility of the one or more metals in the soil results in lower accumulation of the metals by a hyperaccumulator plant of the same metal growing in the soil. In some embodiments, an increase of the pH of the soil decreases the amount of metal accumulated by the hyperaccumulator plant growing in the soil, the mobility of the one or metals released by the weatherable rock, or both. \|[0104] In some embodiments the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to maximize the growth rate of the hyperaccumulator plant. \|[0105] In some embodiments, at least 5 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, at least 10 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 10 tonnes and 100 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 5 tonnes and 10 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 25 tonnes and 50 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 35 tonnes and 40 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 100 tonnes and 200 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, about 150 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 400 tonnes and 800 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. . In some embodiments, about 600 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. \|[0106] In some embodiments, at least about 20 tonnes of nickel hyperaccumulator biomass is grown per hectare. In some embodiments, at least about 400 kg, at least about 500 kg of nickel, at least about 600 kg, at least about 700 kg, at least about 800 kg, at least about 900 kg, or at least about 1,000 kg of nickel is produced per hectare. In other variations, between about 100 kg and 5000 kg, or between 250 kg and 1000 kg, or between 400 kg and 1000 kg of nickel is produced per hectare.\|[0107] In some embodiments, between about 5 tonnes and about 50 tonnes, between about 100 tonnes and about 700 tonnes, between about 500 tonnes and about 700 tonnes, between about 100 tonnes and about 600 tonnes, between about 200 tonnes and about 600 tonnes, between about 300 tonnes and about 600 tonnes, between about 400 tonnes and about 600 tonnes, between about 500 tonnes and about 600 tonnes, between about 100 tonnes and about 500 tonnes, between about 200 tonnes and about 500 tonnes, between about 300 tonnes and about 500 tonnes, between about 400 tonnes and about 500 tonnes, between about 100 tonnes and about 400 tonnes, between about 200 tonnes and about 400 tonnes, between about 300 tonnes and about 400 tonnes, between about 100 tonnes and about 300 tonnes, between about 200 tonnes and about 300 tonnes, or between about 100 tonnes and about 200 tonnes of weatherable rock are mixed into the soil for every hectare on which the hyperaccumulator plant is grown. In some embodiments, about 500 tonnes about 600 tonnes, or about 700 tonnes of weatherable rock are mixed into the soil for every hectare on which the hyperaccumulator plant is grown. \|[0108] In some embodiments, the amount of carbon dioxide sequestered is proportional to the number of Mg2+ ions liberated from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide sequestered per hectare is proportional to the number of Mg2+ ions liberated from the weathering of the weatherable rock mixed into the soil for every hectare. \|[0109] In some embodiments, the amount of carbon dioxide sequestered is proportional to the number of Ca2+ ions liberated from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide sequestered per hectare is proportional to the number of Ca2+ ions liberated from the weathering of the weatherable rock mixed into the soil for every hectare. \|[0110] In some embodiments, the nickel hyperaccumulator plant is harvested mechanically. In some embodiments, the nickel hyperaccumulator plant is harvested manually. In some embodiments, the nickel hyperaccumulator plant is harvested by an automated process. \|[0111] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil. In some embodiments, the plant is irrigated using a drip irrigation system. In some embodiments, the plant is irrigated using sprinkler systems. In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises intermittently irrigating the weatherable rock-enriched soil. In some embodiments, the plant is irrigated using a flood irrigation approach. In some embodiments, the plant is irrigated using traditional irrigation. \|[0112] In some embodiments, the pH of the weatherable rock-enriched soil is above 7. In some embodiments, the pH of the weatherable rock-enriched soil is between 7 and 14. In some embodiments, the pH of the weatherable rock-enriched soil is between 5 and 14. In some embodiments, increasing the content of the weatherable rock of the weatherable rock- enriched soil increases the pH of the soil. \|[0113] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprise drying the nickel hyperaccumulator plant to provide a dried biomass composition; crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a nickel-enriched composition. \|[0114] In some embodiments, the method further comprises quantifying the amount of carbon dioxide that is released or sequestered in one or more steps of any of the methods described herein. In some embodiments, the amount of carbon dioxide released or sequestered by a process is measured directly. In some embodiments, the amount of carbon dioxide released or sequestered by a process is measured using a proxy. In some embodiments, the quantity of Mg2+ is used as a proxy to quantify the amount of carbon dioxide sequestered by chemical weathering of the weatherable rock. \|[0115] In another aspect, provided herein is nickel metal prepared according to any of the methods described above. \|[0116] In another aspect, provided herein is a processed nickel composition comprising a substantially pure nickel, and one or more of the following: Nickel rich ashes also containing K, Ca, oxides (e.g., NiO, MgO), carbonates (e.g., K2CO3, CaCO3, K2Ca(CO3)2), K2SO4, precipitated gypsum, low-mass carboxylic acids, Ni-bearing organic and inorganic compounds. Ni-based compounds such as NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, Ni oxalate, and Ni sulfate. In some variations of the foregoing, the processed nickel composition is at least 15%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 98%, at least 99%, at least 99.8%, at least 99.9%, at least 99.99%, at least 99.999%, or at least 99.9999% pure by weight. In some embodiments, the processed nickel composition is between 15% and 100% pure by weight. \|[0117] In another aspect, provided herein is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: Nickel rich ashes also containing K, Ca, oxides (e.g., NiO, MgO) and carbonates (e.g., K2CO3, CaCCh, KiCa CCh ), K2SO4, precipitated gypsum, low-mass carboxylic acids, Ni-bearing organic and inorganic compounds. Ni-based compounds such as NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, Ni oxalate, and Ni sulfate. In some embodiments, provided herein is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: Ca, Fe, K, Mg, carbonates (e.g., K2CO3, CaCOs, or K2Ca(CO3 ), P, plant cells, C, H, N, O, hydroxyapatite, oxy -hydroxyapatite, or oxides (e.g., NiO, CaO, MgO, or MgNiO2). In some embodiments, the nickel-enriched ash comprises between 5% and 100% nickel by weight. \|[0118] In any of the foregoing embodiments, the weight of nickel refers to the weight of the nickel component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts, respectively, that the nickel is a part of. \|EXAMPLES \|[0119] The presently disclosed subject matter will be better understood by reference to the following Examples, which are provided as exemplary of the invention, and not by way of limitation. \|Example 1: Assessment of weathering rates for different soil and plant configurations\|[0120] Samples of O. decipiens (a close relative to the hyperaccumulator known in the art as O. chalcidica or A. morale) were shipped to a testing facility. There, the seeds were separated from the remainder of the plant biomass, soaked in water to prepare them for germination, and germinated. The germinated seeds were observed to have root systems. Separately, a sample of serpentinite rock was obtained, and was ground into a fine powder, herein referred to as “serpentine soil”. \|[0121] Nine sample planters were prepared, with each planter containing a specific ratio of serpentine soil to potting soil (including both pure potting soil and pure serpentine soil). Seeds of the hyperaccumulator plants were planted in eight of the nine planters, and one planter was left with no seeds, as a control. Additionally, NPK hydroponic fertilizer was added in different concentrations to the continuous, closed-loop irrigation systems of two of the planters. The experimental conditions for each planter are illustrated in FIG. 2. \|[0122] Because Mg2+ is released in the weathering reaction of serpentine, the quantity of Mg2+ leached from the soils in each planter was used as a proxy for the rate of weathering that occurred under each condition. Over the course of 4 months, the total concentration of Mg2+ leached into the closed-loop irrigation system was measured for each of the nine planter conditions shown in FIG. 2. The results of these measurements are shown in FIG. 3. Surprisingly, it was found that quantity of Mg2+ leached by the soil mixtures increased over time as the plants grew. Further, the rate of weathering, as assessed using Mg2+ leaching as a proxy, was found to correlate to plant biomass growth. \|Example 2: Field-scale enhanced rock weathering experiment \|[0123] A field-scale trial was employed to investigate the synergistic combination of nickel phytomining and enhanced weathering. The principal aim of this experiment was to evaluate the scope for nickel extraction by the hyperaccumulator plant Odontarrhena decipiens and to quantify the carbon capture potential of crushed serpentinite rock added to the naturally occurring serpentine agricultural soil. \|[0124] A 112 m x 168 m field site was selected for this trial based on aerial photography and ground observations. Four permanent reference points for determining precise locations were established by cementing steel posts into the ground at the comers of the field site. The area was then partitioned into four equally-sized rectangular blocks, each measuring 56 m x 84 m. A scale diagram of the randomized complete block design used in the trial is shown in FIG. 4. These blocks represent replicates, such that each block contained eight randomized 12 m x 18 m plots (one for each of the eight rock treatments) separated by an 8 m margin of untreated land. The amount of rock treatment added to each plot as measured in tonnes of serpentinite rock per hectare is shown in FIG. 4. The randomized complete block design accounts for the effects of extraneous variables (e.g. hydrological gradients across the site) and hence, mitigates bias caused by inherent variation. \|[0125] The entire field site was tilled prior to the trial. Crushed serpentinite rock was sourced from a nearby quarry and applied by hand to the soil surface of each plot at rates ranging from 9.375 to 600 tonnes per hectare, whereby the next higher rate was set to be double the previous as illustrated in FIG. 4. Each block also contains a ‘control’ treatment where no serpentinite rock is added (i.e. 0 tonnes per hectare), against which all other treatments were compared statistically. The applied rock material was incorporated into the soil to an approximate depth of 150 mm using a rotavator. One-year-old Odontarrhena decipiens specimens were then transplanted into each plot, in thirteen rows with 1 m rowspacing and 0.5 m spacing between the individual plants. Organic fertilizers, pesticides, and fungicides were added to the experimental plots to ensure baseline crop performance and mitigate pest/pathogen interference in all treatments. \|[0126] At the beginning of the experiment, over a hundred mesh bags were filled with 0.4 g of crushed serpentinite and buried in the plots at soil depths between 50-200 mm. Retrieval of the grains from these bags at the end of the trial permits the direct assessment of mineral weathering through X-ray analysis. \|Soil sample collection and measurements \|[0127] Before applying the serpentinite rock material, fifteen baseline soil samples were collected from each block using a steel auger and following a W-shaped sampling pattern. These initial (pre-planting, pre-rock application) soil samples are taken from three depths: 0- 0.3 m, 0.3-0.6 m, and 0.6-0.9 m. Soils are then passed through a 2 mm mesh size sieve, air dried, and tested for the following physical and chemical parameters: pH (in H2O and IM KC1); organic matter and humus %; plant-available nitrogen, phosphorus and potassium; soil texture (sand/silt/clay %); cation exchange capacity; and, total and plant-available Ca, Mg, K, Na, Fe, Cd, Co, Cr, Cu, Mn, Ni, Pb, and Zn. Further soil samples were collected monthly from each of the thirty-two experimental plots and tested for pH, electrical conductivity, cation exchange capacity, and plant-available cations. These data were used to monitor changes in the concentrations of plant-available nutrients and nickel over time, and to estimate rock weathering and carbon dioxide capture rates via a conventional mass balance approach, in combination with novel quantification methods. \|Plant sample collection and measurements \|[0128] Aboveground plant tissues are harvested from all plots after a suitable time (e.g., approximately 6-8 months) after the trial began. Plant materials are dried and weighed to determine crop yields, and ground for analysis of nutrients and metals. These data are used to measure the efficiency of nickel uptake by the hyperaccumulator plants, and to evaluate the correlation between rock application and nickel uptake rates. Moreover, values for total uptake of calcium, magnesium, potassium and sodium are fed into mass budget calculations for carbon capture quantification. \|[0129] Aboveground plant tissues were harvested from five different mature hyperaccumulator plant specimens randomly selected from all plots after a suitable time (e.g., approximately 6-8 months) after the trial began. Plant samples were washed with distilled water, dried in a forced-air oven at 60 °C for 48 hours, and powdered separately using a laboratory grinding mill. These plant samples were used to determine total heavy metal concentrations in the plant tissues. \|Soil pH and electrical conductivity measurements \|[0130] The pH and the electrical conductivity (EC) of the soil samples determined using a Combined Conductivity /pH Meter equipped with a temperature input, which internally corrects for the effect of temperature on measured values. pH and EC were standardized using a 3-point calibration protocol with certified reference solutions (buffers at pH 4.00, 7.00, and 14.00; EC standards at 12.88 mS, 1413 pS, and 84 pS). To streamline the measurements, pH and EC were tested sequentially from the same sample. For each soil sample, 15.0000 ± 0.0005 g of soil was weighed into a 50 mL polypropylene centrifuge tube and combined with 30.0000 ± 0.0150 mL of ultrapure water (resistivity of 18.2 MQ-cm at 25 °C). The tubes were stoppered, agitated on a rotary shaker for 3 minutes, unstoppered and then left to equilibrate with the atmosphere for 30 minutes. An additional three replicates of control soil (initial/baseline soil containing no additives) were prepared and used to precondition the pH and conductivity electrodes prior to analysis of the experimental samples. This preconditioning process shortens the timescales for stable measurements and mitigates measurement error in the first few experimental samples (e.g. due to contamination with trace amounts of buffer solution). To obtain pH measurements, the pH electrode was swirled into the soil-water mixture’s supernatant for 10 seconds, and then gently released into the slurry until the instrument identified that a stable pH reading was achieved (or 3 minutes after initial insertion, where stabilization was not achieved). pH measurements were recorded to 0.001 pH units, and the electrode was rinsed thoroughly with ultrapure water between samples. To obtain EC measurements, the conductivity electrode was inserted into the soilwater mixture’s supernatant and held until the instrument indicated that a stable EC reading was achieved (or 1 minute after initial insertion, where stabilization was not achieved). EC measurements were recorded to four significant figures, and the electrode was rinsed thoroughly with ultrapure water between samples. \|Soil analysis methods for total heavy metals \|[0131] The soil samples were tested for total heavy metals by first drying a test portion of the soil and reducing the grain size of the soil to below a particle size of 250 microns. Each test portion of the soil was then weighed (0.5 g to 1.0 g based on dry mass) and transferred to a microwave extraction vessel. A few drops of water were then added to the extraction vessel before adding a HC1 and nitric acid solution and mixing well. The temperature of the extraction mixture was increased at a rate of approximately 10 °C/min to 175 ± 5 °C using a microwave digestion system. The amount of total Ni in the soil samples was then determined using ICP-OES. \|Availability ofNi with Mehlich-1 digestion \|[0132] The soil samples were prepared by mixing 5 g of the soil samples with 20 mL of a Mehlich-1 extraction solution consisting of a mixture of HC1 and H2SO4. The mixture was then stirred for 5 min at 180 cycles/min after which the suspension was allowed to rest for 16 h before decanting off the supernatant The total amount of Ni in the soil samples was then determined by testing an aliquot of the supernatant using ICP-OES. \|Other analytical methods \|[0133] It should be understood that one or more additional techniques may be used to determine the amount of Ni in the soil, the amount of rock-derivable cations in the tissue of the hyperaccumulator plants or the soil, the amount of heavy metals in the tissue of the hyperaccumulator plants or the soi, the pH of the soil, the electrical conductivity of the soil, and other aspects of the weatherable rock, soil, and hyperaccumulator plants, including quantification of the weathering rate. For example, X-ray fluorescence analysis of weathered rock material (retrieved from mesh bags buried in the plots) is used to quantify changes in grain surface chemistry. These data provide an independent method for mineral weathering rate quantification. The loss of cations from the added rocks may serve as a proxy for the accumulation of cations released from this process in the plant and soil. \|Determination of total heavy metal and Ca, Mg, K concentrations in plants with digestion\|[0134] Aboveground plant tissues were digested in an acid solution (HNO3 65% and H2O2 30%) using a microwave digestion system to determine total heavy metal concentrations in plants. A sample of the plant matter (300 mg) was mixed with 2 mL of HNO3 and 2 mL of H2O2, stirred for at least 20 min, and then digested using a microwave digestion system. Plant tissue samples calibration curves were plotted from Ni concentrations of 2, 4 and 6 mg/L. The solution was diluted 20 times. The amount of Ni in the plant tissue samples was then determined using ICP-OES. \|Results and Analysis \|[0135] Approximately 8 months after the trial began, representative soil samples were collected from the plots for analysis. As shown in FIG. 5, increasing serpentinite application rates resulted in increasing soil pH. Moreover, application rates above 0.9375 kg m 2 resulted in statistically significant increases in soil pH with respect to the control soils, where no serpentinite rocks were added, which is evidence of chemical weathering of the added serpentinite rock. Surprisingly, soil pH continued to increase with increasing application rates, and rose substantially to the highest recorded level at the highest application rate (60 kg m 2) as shown in FIG. 5. Chemical weathering of the added alkaline minerals (e.g. serpentinite rock) will lead to carbon dioxide sequestration. Enhanced weathering of the added rock material is also supported by evidence of elevated soil electrical conductivity (EC) following rock applications as shown in FIG. 6. Higher EC indicates the release of cations due to rock dissolution, and similarly represents evidence for chemical weathering of the serpentinite rock applied to the soil. This chemical weathering leads to carbon dioxide sequestration. \|[0136] Amendment of soils with serpentinite rock also resulted in higher nickel uptake into the tissues of the hyperaccumulator plants as compared to the hyperaccumulator plants grown in the control soils, with the highest nickel yields observed in soils amended with 3.75 to 15 kg m 2 of serpentinite rock as shown in FIG. 7. The mean total Ni yield from the hyperaccumulator plants was calculated by multiplying the (dry) biomass yield by the (dry) biomass Ni concentration. Mean total Ni yields from the hyperaccumulator plants ranged from around 1.4 g Ni m 2 (14 kg Ni ha 1) in the control plots to a peak of about 2.5 g Ni m 2 (25 kg Ni ha 1) in the plots treated with 15 kg m 2 (150 t ha 1) of serpentinite rock. Plants grown on soils with elevated pH will typically accumulate less nickel. Surprisingly, nickel yields increased in the soils amended with 3.75 to 15 kg m 2 of serpentinite rock, which implies that the combination of enhanced weathering of serpentinite and nickel hyperaccumulators realized a synergistic benefit. Overall, this data indicates mass transfer of Ni from the applied serpentinite rock into the tissues of the hyperaccumulator plants. \|[0137] Timeseries data for soil-extractable Ni was determined by a Mehlich 1 extraction procedure and confirms that soil concentrations increased in all plots treated with serpentinite rock between when the trial began (0 m) and the following spring (~5 m), when the hyperaccumulators would have exhibited low primary production as shown in FIG. 8. However, the subsequent steep reduction in soil Ni concentrations between spring (~ 5 m) and mid-summer (~7 m) is evidence for the uptake of soil Ni and depletion of the soil Ni pool by the hyperaccumulator plants at a time of increasing primary productivity as shown in FIG. 8. This data is evidence of the synergy between the two processes because depletion of the soil nickel pool by hyperaccumulator plants can be offset through the weathering of additional nickel bearing-minerals (e.g., serpentinite) introduced to the soil, resulting in carbon negative nickel recovery. \|Statistical analyses \|[0138] Statistical analysis was also performed to determine the significance of the relationships between rock application, plant nickel uptake, and (potential) carbon capture rates. Statistical analysis of the soil data was performed using a linear mixed model with fixed model Treatment * Time and random model of Block/Plot. Where appropriate, variables were first transformed to ensure homogeneity of variance. F statistics were obtained using the Kenward-Roger approximation. Statistical analysis of the plant data was performed using a linear model accounting for differences between blocks. A third order polynomial was fitted over application rate with highest order terms successively dropped if found to be non- significant. \|[0139] Regarding soil pH, statistically significant differences were observed both between treatments (F4, 12=21.54, p < 0.0001) and over time (F3, 45=7.18, p=0.0005). Predicted means and standard errors for each significant main effect is shown in FIGS. 9 and 10. For Soil EC, statistically significant differences were observed both between treatments (F4, 12=3.28, p = 0.049 - a marginal effect) and over time (F3, 45=8.59, p=0.0001). Predicted means and standard errors for each significant main effect are shown FIGS. 11 and 12. For ammonium acetate (AA) extractable nickel, statistically significant differences were observed both between treatments (F4, 12=5.66, p = 0.008) and over time (F3, 45=10.03, p<0.0001). Predicted means and standard errors for each significant main effect is shown in FIGS. 13 and 14. For ammonium acetate extractable magnesium, a statistically significant interaction effect was found between treatment and sampling date (F12,45=2.27, p=0.02). Overall, the largest effect is attributed to differences over time (F3, 45=6.81, p=0.007). Predicted means and standard errors are shown in FIG. 15. A multivariate correlation figures between all soil data can be seen in FIG. 16. \|[0140] The above preliminary data was collected over the first 8 months of the field trial experiment. Additional data will be gathered until 12 months after the start of the field trial experiment to further elucidate the relationship between the application rate of the weatherable rock and the accumulation of metal by the hyperaccumulator plant, the soil pH, the soil electrical conductivity, the weatherable rock-derivable cations in the soils and plants, and the heavy metals in the soils and the plants, as well as determining the weathering rate of the weatherable rock, the amount of nickel ore extractable from the plants, and quantifying the amount of carbon dioxide sequestered. \|Example 3: Field-scale enhanced rock weathering experiment with two controls\|[0141] In this example, a field- scale trial is employed to further investigate the synergistic combination of nickel phytomining and enhanced weathering. A scale diagram of the randomized complete block design used in the trial is shown in FIG. 17. The trial uses an approximately level 112 m x 208 m field site that is divided into four blocks of equivalent area, each measuring 56 m x 104 m, with every block subdivided into 10 randomly-assigned 12 m x 18 m plots representing the ten treatments as shown in FIG. 17. The amount of rock treatment added to each plot as measured in tonnes of serpentinite rock per hectare is shown in FIG. 17. Neither rock nor hyper- accumulator plants are added to the plots marked with ‘XX’ in FIG. 17. These plots are designed to simulate native soil conditions. The plots are segregated by an 8 m margin of untreated land. \|[0142] Two control treatments are included in this study: a rock-free control (i.e. 0 tonnes of rock added per hectare) where hyperaccumulator plants are grown, and a second control where no plants, rock amendments, or management practices are employed, as denoted by ‘XX’ in FIG. 5. The rock-free control is used to assess the effect of different rock applications on nickel uptake efficiency and carbon capture. The experiments with no plants, rock amendments, or management practices control serves a baseline (the native soil’s background conditions). \|Soil sample collection and measurements \|[0143] Following a W-shaped sampling pattern, multiple baseline soil samples are collected and aggregated from each of the forty plots at three discrete depths (0-0.3, 0.3-0.6 and 0.6-0.9 m) using a steel auger. These initial soil samples are separately homogenized, passed through a 2-mm mesh size sieve, and air-dried. Soils are then tested for pH (in H2O and IM KC1) and electrical conductivity (in H2O); inorganic/organic carbon and nitrogen %; plant-available nitrogen, phosphorus and potassium; soil texture (sand/silt/clay %), bulk density and water holding capacity; cation exchange capacity and exchangeable acidity; major oxide and soil mineralogy %; and, total and plant-available Ca, Mg, K, Na, Fe, Cd, Co, Cr, Cu, Mn, Ni, Pb, and Zn. Further soil samples are taken at bi -monthly intervals and tested to determine changes in fundamental soil parameters (pH, electrical conductivity, organic/inorganic carbon) and the concentration of exchangeable (plant- available) metals. These data are critical for monitoring changes in nickel availability and carbon dioxide capture rates in the plots. \|Plant sample collection and measurements \|[0144] Approximately 1-year after the start of the field trial, shoot tissues are harvested from all plots, and the shoot tissues are dried and weighed to quantify crop performance. In addition, plant materials are powdered, digested, and tested to determine metal content and analyze the correlation between rock application rate and nickel uptake efficiency. Total plant calcium, magnesium, potassium, and sodium values are added to the respective values from the soil analyses of exchangeable elements, which together enable the quantification of rock weathering and carbon capture rates. \|Aqueous sample collection and measurements \|[0145] Pore water samples are extracted from the soil using lysimeters installed in the plots. These aqueous samples are analyzed for changes in the following parameters: pH, electrical conductivity, and alkalinity; and dissolved cations (e.g. nickel, magnesium) and anions (e.g. chloride, nitrate). These data are essential for accurate monitoring of rock dissolution, nickel release, and carbon capture rates. Soil-atmosphere greenhouse gas sample collection and measurements \|[0146] Gaseous samples are collected during the trial using static chambers installed in the plots and are analyzed using gas analysis mass spectrometry to determine soil-atmosphere fluxes of major greenhouse gasses, such as carbon dioxide, methane, and nitrous oxide. This example seeks to determine the effects of the addition of alkaline rocks to the soil on overall emissions of potent non-CCh greenhouse gasses, and thus impact on climate change. These gas measurements are performed in serpentine soils, and also provide evidence that the soil amendments and agricultural management practices associated with the trial result in the conversion of existing soil organic carbon into atmospheric carbon dioxide. \|Example 4: Life Cycle Assessment at Kilotonne and Megatonne Scales Per Year\|[0147] A Life Cycle Assessment (LCA) was employed to ensure that the enhanced rock weathering/hyperaccumulator plant operation is sufficiently CO2 negative at the necessary scale. The aim was to model the net sequestration of 1 kilotonne and 1 megatonne of CO2 per year. The LCA was conducted using SimaPro software which draws data from various databases. The study adopted a cradle-to-gate approach, which includes all the major processes in the life cycle from the mining operation to the production of nickel ore, however the environmental impact of waste treatment was excluded from the LCA due to the ambiguity of its relevance. The two products of the operation are CO2 uptake (carbon dioxide removal through enhanced rock weathering) and the production of nickel ore through phytomining. The major processes within the established system boundaries include the mining, crushing, and milling of serpentine, the transportation of the serpentine rock to the site of placement, the fertilizer used, and harvesting, drying, and combustion of the hyperaccumulator plants. A unit area of land was used as the functional unit for the LCA to account for both the CO2 extraction and the nickel ore production. For example, per every m2 of area of serpentine soil used for the cultivation of A. Murale (or a similar hyperaccumulator plant), a certain amount of nickel will be produced and a certain amount of CO2 will be sequestered. This functional unit ensures that neither of the two products of the system (i.e. CO2 uptake and the production of nickel ore) are neglected from the LCA analysis and that their amounts are calculated independently of each other. \|[0148] The data used for the LCA was collected from several sources and the model was built on the basis of existing models. The data related to standard transportation, machinery, energy, and materials were kept as they were in the models, apart from several necessary adjustments to bring the model closer in line with the operation. For example, during the whole process, the electricity comes from the grid, where it is mostly produced using hydropower. This feature was reflected in the model. It is not required that hydropower be utilized in the process, though it will lower the net negative efficiency. A range of parameters, such as the weathering rate and serpentine content in soil, was introduced into the model. The information used to determine the parameter values was sourced from a combination of existing literature on similar experiments with hyperaccumulators and mineral weathering. The firm relied on rates of natural weathering processes which resulted in calculations that predict significant CO2 uptake and nickel production. \|[0149] The models for 1 kilotonne-scale production yearly can be seen in FIG. 18. The 1 megatonne-scale chart can be seen in FIGS. 19A and 19B. The main difference between the operations is the increased transport distance between the serpentine mining site and the farming sites in the megatonne- scale model as compared to thel kilotonne-scale model. Although not incorporated into the model, utilizing renewable energy for transportation of the rock between the mining site and farming sites would help ensure that the process remains CO2 negative even with long transportation distances. According to this LCA study, the operation can run at scale at an approximately 90% net efficiency in terms CO2 sequestration; additional details of the LCA study can be found in FIG. 20.	Family Number\|(108265090)\|108265090\|Object of Invention\|(WO202420548 A2)\| (...) particles to increase reactive mineral surface area, dispersing the weatherable rock particles into the soil within a plot of land, planting nickel hyperaccumulating plants onto the plot of land to capture the nickel released from the weatherable rock during chemical weathering.\|Abstract\|(ID202507231 A)\|Methods are provided for extracting metals from rocks and sequestering (capturing and storing) carbon dioxide. In some embodiments, methods are provided to use phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. Compositions are also provided, which include metal compositions made by the methods here. Provided are methods of extracting metals from rocks and sequestering carbon dioxide. In some embodiments, provided are methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. Provided are also compositions, including metal compositions produced by the methods herein.\|Independent Claims\|(WO202420548 A2)\| (...) weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide by converting carbon dioxide to bicarbonate or carbonate; and extracting and processing the released metal to provide a metal-enriched composition.\|	Chemical engineering\|Environmental technology\|Materials, metallurgy	C22B-001/00\|C22B-001/14\|C22B-003/08\|C22B-003/26\|C22B-003/42\|C22B-003/44\|C22B-023/043\|C22B-023/0453\|C22B-023/0461\|C22B-026/22\|C25C-001/08\|Y02C-020/40		C22B-001/00\|C22B-001/14\|C22B-003/08\|C22B-003/26\|C22B-003/42\|C22B-003/44\|C22B-023/043\|C22B-023/0453\|C22B-023/0461\|C22B-026/22\|C25C-001/08\|Y02C-020/40	B01J-047/02\|B09C-001/00\|C01G-053/00\|C22B-003/00\|C22B-003/04\|C22B-003/08\|C22B-003/18\|C22B-003/44\|C22B-007/00\|C22B-023/00	B01J-047/02\|B09C-001/00\|C01G-053/00\|C22B-003/00\|C22B-003/04\|C22B-003/08\|C22B-003/18\|C22B-003/44\|C22B-007/00\|C22B-023/00					US6159270\|US6786948	US6159270 60049318 WHO=Examiner SELF=N CAT=A\|US6786948 1414600 WHO=Examiner SELF=N CAT=A		XP093159640; XP087050049; XP093159650; XP093159654; US6159270; US6786948\|\|\|	\|(WO2024/020548)\|International Search Report [Examiner]\|-CRISTINA BECERRA-CASTRO: "Bacterially Induced Weathering of Ultramafic Rock and Its Implications for Phytoextraction", APPLIED AND ENVIRONMENTAL MICROBIOLOGY, AMERICAN SOCIETY FOR MICROBIOLOGY, US, vol. 79, no. 17, 1 September 2013 (2013-09-01), US , pages 5094 - 5103, XP093159640, ISSN: 0099-2240, DOI: 10.1128/AEM.00402-13\|-JALLY BASTIEN; FRANÇOIS MATHILDE; KESSLER MORGANE; LAUBIE BAPTISTE; SIMONNOT MARIE-ODILE: "Recovery of nickel from strongly acidic bio-ore leachate using a bispicolylamine-based chelating resin", SEPARATION AND PURIFICATION TECHNOLOGY, ELSEVIER SCIENCE, AMSTERDAM, NL, vol. 293, 20 April 2022 (2022-04-20), NL , XP087050049, ISSN: 1383-5866, DOI: 10.1016/j.seppur.2022.121126\|-TIMOTHY LENTON: "First plants cooled the Ordovician", NATURE GEOSCIENCE, no. 5, 1 February 2012 (2012-02-01), pages 86 - 89, XP093159650, DOI: 10.1038/ngeo1390\|-PETRA SUSAN KIDD: "Developing Sustainable Agromining Systems in Agricultural Ultramafic Soils for Nickel Recovery", FRONTIERS IN ENVIRONMENTAL SCIENCE, FRONTIERS MEDIA, vol. 6, XP093159654, ISSN: 2296-665X, DOI: 10.3389/fenvs.2018.00044\|\|\|	PENDING	(EP4558651)\|PENDING\|(WO2024/020548)\|LAPSED\|(ID2025/07231)\|PENDING\|(TW202417649)\|PENDING	ALIVE	(EP4558651)\|ALIVE\|(WO2024/020548)\|DEAD\|(ID2025/07231)\|ALIVE\|(TW202417649)\|ALIVE	(EP4558651)\|LEGAL DETAILS FOR EP4558651\|Actual or expected expiration date=2043-07-21\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-07-21\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP23843926\|Application date=2023-07-21\|Standardized application number=2023EP-0843926\|Event publication date=2024-01-26\|Event code=EP/STAAPCT\|Event group=Examination events Entry into national phase\|The international publication has been made\|Original code: STAA\|Event publication date=2025-04-25\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN 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expiration date=2043-07-21\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-07-21\|Event code=TW/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=TW TW112127364\|Application date=2023-07-21\|Standardized application number=2023TW-0127364\|Event publication date=2024-05-01\|Event code=TW/A\|Event indicator=Pos\|Event group=Examination events\|Laid open application for patent or patent of addition\|Publication country=TW\|Publication number=TW202417649\|Publication stage code=A\|Publication date=2024-05-01\|Standardized publication number=TW202417649	(EP4558651)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4558651)\|Extension States: BA\|(EP4558651)\|Validation States: MA, MD, TN, KH\|(WO2024/020548)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2024/020548)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2024/020548)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2024/020548)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2024/020548)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP4558651)\|EP\|(WO2024/020548)\|EP; ID\|(ID2025/07231)\|ID\|(TW202417649)\|TW	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=nwH/nfofj4/DzwgmQHVFUW8tmrmn8uQzNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006462121&ekey=2357&xpn=EP4558651&kind=A2	https://register.epo.org/application?number=EP23843926	https://permalink.orbit.com/RenderStaticFirstPage?XPN=0hvHXPoHlmIuw56Xk6cpNXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2024/020548)\|US\|(WO2024/020548)\|US\|(TW202417649)\|US	(WO2024/020548)\|NAME=METALPLANT PUBLIC BENEFIT CORPORATION 2810 N Church St PMB 88709 Wilmington, Delaware 19802-4447 , COUNTRY=US\|(WO2024/020548)\|NAME=METALPLANT PUBLIC BENEFIT CORPORATION 2810 N Church St PMB 88709 Wilmington, Delaware 19802-4447 , COUNTRY=US\|(TW202417649)\|NAME=METALPLANT PUBLIC BENEFIT CORPORATION , COUNTRY=US	(EP4558651)\|GB\|(WO2024/020548)\|US\|(WO2024/020548)\|US\|\|	(EP4558651)\|NAME=J A Kemp LLP 80 Turnmill Street , CITY=London EC1M 5QU , COUNTRY=GB , REG=101669666\|(WO2024/020548)\|NAME=ROBERTS, Emily Jane et al. Morrison & Foerster LLP 425 Market Street San Francisco, California 94105 , POSTCODE=94105 , COUNTRY=US\|(WO2024/020548)\|NAME=ROBERTS, Emily Jane et al. Morrison & Foerster LLP 425 Market Street San Francisco, California 94105 , POSTCODE=94105 , COUNTRY=US\|(ID2025/07231)\|NAME=Marolita Setiati\|(TW202417649)\|NAME=CHEN, CHANG-WEN NAME=CHANG, CHE LUN NAME=LO, WEN-MIAO	(EP4558651)\|US; US\|(WO2024/020548)\|US; US\|(WO2024/020548)\|US; US\|\|(TW202417649)\|US; US	(EP4558651)\|NAME=MATZNER, Eric Jason, CITY=Wilmington, Delaware 19802-4447, COUNTRY=US \|NAME=WASSERSON, Laura R., CITY=Wilmington, Delaware 19802-4447, COUNTRY=US\|(WO2024/020548)\|NAME=MATZNER, Eric Jason c/o MetalPlant Public Benefit Corporation 2810 N Church St, PMB 88709 Wilmington, Delaware 19802-4447, POSTCODE=19802-4447, COUNTRY=US \|NAME=WASSERSON, Laura R. c/o MetalPlant Public Benefit Corporation 2810 N Church St, PMB 88709 Wilmington, Delaware 19802-4447, POSTCODE=19802-4447, COUNTRY=US\|(WO2024/020548)\|NAME=MATZNER, Eric Jason c/o MetalPlant Public Benefit Corporation 2810 N Church St, PMB 88709 Wilmington, Delaware 19802-4447, POSTCODE=19802-4447, COUNTRY=US \|NAME=WASSERSON, Laura R. c/o MetalPlant Public Benefit Corporation 2810 N Church St, PMB 88709 Wilmington, Delaware 19802-4447, POSTCODE=19802-4447, COUNTRY=US\|(ID2025/07231)\|NAME=MATZNER Eric Jason\|NAME=WASSERSON Laura R\|(TW202417649)\|NAME=MATZNER ERIC JASON, COUNTRY=US \|NAME=WASSERSON LAURA R, COUNTRY=US		3	4			(EP4558651)\|WO2024/020548\|(ID2025/07231)\|WO2024/020548		(WO2024/020548)\|Number of Claims: NCL=1\|\|(WO2024/020548)\|Number of Claims: NCL=28\|Extended kind: EXTK=z\|\|(TW202417649)\|Number of Claims: NCL=28\|		(EP4558651)\|ENGLISH (ENG)	(ID202507231)\|Patent\|(EP4558651)\|Patent\|(TW202417649)\|Patent\|(WO202420548)\|Patent\|(WO202420548)\|Patent	Titre: (EP4558651)\|Methods for obtaining carbon neutral or carbon negative metals from plants, and related compositions Résumé: (EP4558651)\|Provided are methods of extracting metals from rocks and sequestering carbon dioxide. In some embodiments, provided are methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. Provided are also compositions, including metal compositions produced by the methods herein.	34	Abstract	gpt-4o-mini	uncertain	The article mentions sequestering carbon dioxide in the context of extracting metals from ultramafic rocks, but it does not explicitly focus on accelerated weathering or the specific processes related to mineral carbonation.
35	CN201510055353	CN201510055353	CN104696005\|CN104696005	69557757	CN104696005 B 2016-08-31 [CN104696005B]\|CN104696005 A 2015-06-10 [CN104696005]	2015-02-03	2015-02-03	2016-08-31\|2015-06-10	(CN104696005B)\|2016-08-31	(CN104696005)\|2035-02-03	(CN104696005)\|Method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in old goaf of coal mine	(CN104696005)\|The invention discloses a method for synchronously extracting residual coalbed methane and sealing and preserving carbon dioxide in an old coal mined-out area of coal mine. The method comprises the following steps: during working face mining, a pipeline is paved at the bottom of a mining roadway, seam grooves are axially formed in the pipeline at intervals, baffles are arranged on both ends of each seam groove, high-pressure hoses are respectively wound on the seam grooves, water under a certain pressure is injected in the high-pressure hoses to perform 'yielding' protection on the pipeline, so that crushed coal and rock in the mined-out area can be prevented from destroying the pipeline and blocking air holes; after working face mining is finished, a fire dam is arranged at a mining stop line, the pipeline is communicated to the ground, and well drilling is constructed from the ground to the upper part of the mined-out area; CO2 is injected from the ground to the mined out area along the pipeline, because the density of the CO2 is larger than CH4, and the crushed coal and rock remained at the bottom of the mined-out area has higher adsorptivity to CO2, the absorbed CH4 is replaced out and is accumulated at the top of the mined-out area, and the accumulated CH4 is extracted by well drilling. The method has dual benefits of sealing and preserving the carbon dioxide, and developing and utilizing the residual coalbed methane.	TAIYUAN UNIVERSITY OF TECHNOLOGY	(CN104696005)\|TAIYUAN UNIVERSITY OF TECHNOLOGY ([CN])\|(CN104696005)\|TAIYUAN UNIVERSITY OF TECHNOLOGY	HU SHENGYONG\|GAO QIANG\|CHEN CHUNJIAN\|ZHANG XIANG	(CN104696005)\|HU SHENGYONG\|GAO QIANG\|CHEN CHUNJIAN\|ZHANG XIANG\|(CN104696005)\|HU SHENGYONG\|GAO QIANG\|CHEN CHUNJIAN\|ZHANG XIANG	(CN104696005)\|LU MAOCHUN;KERUIDA PATENT AGENCY CO., LTD. TAIYUAN CITY\|Reg. Nb: 14101		(CN104696005)\|1. The method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in the old goaf of the coal mine is characterized by comprising the following steps:a. in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) from a position 5-10 m away from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5);b. tightly winding a high-pressure hose (7) with the diameter of 5-15 cm and the compressive strength of 5-10 MPa on the slot (5), injecting 2-5 MPa high-pressure water into the high-pressure hose (7) when all pipelines (4) wound with the high-pressure hose (7) enter a goaf (8), and bundling a water injection port of the high-pressure hose (7) after water injection is finished;c. after the stoping of the working face (1) is finished, a closed wall (10) with the thickness of 2-5 m is arranged at the stoping line (9), and the pipeline (4) penetrates through the closed wall (10) and is connected to the ground (11) and the CO2A gas storage tank (12) is communicated with CO2A first valve (13) is arranged at an air outlet of the air storage tank (12);d. constructing a well (14) downwards from the ground (11) every 200-300 m along the middle of the goaf (8) until the bottom of the well (14) is 20-40 m away from the upper part of the goaf (8), inserting an extraction pipe (16) into the well (14) from the ground (11), and arranging a second valve (17) at the upper end of the extraction pipe (16);after the well mouth of the drilling well (14) is sealed, an extraction pipe (16) is connected with a pump station (15);e. opening a first valve (13) by CO2The gas storage tank (12) injects CO into the goaf (8) along the pipeline (4)2Simultaneously opening a second valve (17) to begin extracting CO in the goaf (8)2Displacing residual coal bed gas;f. when extracting CO in the pipe (16)2When the concentration is higher than 10%, the first valve (13) and the second valve (17) are closed, and the CO injection is stopped2And extracting residual coal bed gas.\|	(CN104696005)\|The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction, which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf.\|the invention discloses a method for cooperatively sealing carbon dioxide and developing residual coalbed methane in a coal mine goaf, which comprises the following steps: in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) at a distance of 5-10 m from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5).\|	(CN104696005)\|COALBED GAS(100,12)\|OLD GOAF(100,10)\|COAL MINE(100,8)\|COAL MINE OLD GOAF(100,6)\|EXTRACTING RESIDUAL COALBED GAS(100,6)\|RESIDUAL EXTRACTION(100,6)\|SEALING(100,4)\|METHANEDIONE(100,3)\|METHANEDIONE COOPERATIVE SEQUESTRATION(100,1)\|STOPING ROADWAY(84,4)\|METHANEDIONE SEQUESTRATION(73,3)\|RESIDUAL COALBED METHANE(66,4)\|PIPELINE(60,23)\|SEQUESTERING CO OPERATIVE(58,1)\|RESIDUAL COALBED METHANE DEVELOPMENT(57,1)\|GOAF(53,22)\|RESIDUAL COALBED METHANE EXTRACTION(53,2)\|GOAF MIDDLE(52,1)\|METHANEDIONE SEQUESTRATION DOUBLE BENEFIT(51,1)\|EXTRACTION PIPE(46,10)\|ADSORBED CH4AND(46,1)\|WORKING FACE STOPING(43,4)\|WORKING FACE(39,6)\|CH4AND BROKEN COAL(38,1)\|METHANE EXTRACTION(37,1)\|SLIT GROOVE(35,2)\|BAFFLE(33,3)\|SEALING METHANEDIONE(33,2)\|CUTTING HOLE(31,3)\|RESIDUAL COALBED GAS(29,3)\|STOPING(26,4)\|BROKEN COAL ROCK(25,3)\|WORKING FACE STOPING(25,2)\|CO2A GAS STORAGE TANK(25,1)\|RESIDUAL COALBED GAS UTILIZATION(25,1)\|PIPE WALL(24,3)\|CLOSURE WALL(22,2)\|PIPELINE2DUE(22,1)\|DUAL BENEFIT(19,1)\|EXTRACTING(18,2)\|CO2THE GAS STORAGE TANK(17,4)\|STOPING LINE(17,4)\|GAS STORAGE TANK(13,7)\|NONPRODUCTIVE COAL SEAMS2OUTSTANDING(13,1)\|COMPRESSIVE STRENGTH(12,3)\|WATER INJECTION(10,5)\|PUMP STATION(10,4)\|METHANEDIONE SEQUESTRATION BENEFIT(10,1)\|SEALING WALL(9,6)\|WELL DRILLING(9,6)\|AIR STORAGE TANK(9,3)\|RESIDUAL COALBED METHANE RESOURCE(9,1)\|AIR OUTLET(8,2)\|CO2HAS STRONG ADSORBABILITY(8,1)\|COAL PILLAR CRACK(8,1)\|ADSORBED CH4IS(7,1)\|CH4THE PROMINENCE(7,1)\|CO2DENSITY OFGREATER(7,1)\|CO2FOR DISASTER(6,1)\|COAL SEAM STORE CO2CO(6,1)\|GEOLOGICAL DISPOSAL(6,1)\|MINE ROADWAY(6,1)\|VENTILATION BURDEN(6,1)\|IGNITION PHENOMENON NATURE(5,1)\|INTRODUCING CO2SEALING(5,1)\|RELEVANT SCIENTIST(5,1)\|ABANDONED RESIDUAL(4,1)\|COAL MINING RAPID DEVELOPMENT(4,1)\|COAL RESIDUE(4,1)\|DISPLACING RESIDUAL COALBED GAS(4,1)\|GLOBAL CONCERN(4,1)\|RESIDUAL DISPLACEMENT(4,1)\|STORE CO2IT(4,1)\|ADSORPTIVITY(3,1)\|ATMOSPHERE2THE(3,1)\|DUCT SLOT(3,1)\|GOAF4THE GAS EXTRACTION(3,1)\|LIVING ENVIRONMENT(3,1)\|PIPE PROTECTION(3,1)\|SIGNIFICANCE(3,1)\|UNSAFE FACTOR(3,1)\|ADDITIVE(2,1)\|COAL ROCK MASS PAIR(2,1)\|COALBED GAS INDUSTRY(2,1)\|FACE EXTRACTION(2,1)\|FLEXIBLE PIPE(2,1)\|GLOBAL CLIMATE(2,1)\|\|(CN104696005)\|COALBED GAS(100,12)\|OLD GOAF(100,10)\|COAL MINE(100,8)\|COAL MINE OLD GOAF(100,6)\|EXTRACTING RESIDUAL COALBED GAS(100,6)\|RESIDUAL EXTRACTION(100,6)\|SEALING(100,4)\|METHANEDIONE(100,3)\|METHANEDIONE COOPERATIVE SEQUESTRATION(100,1)\|STOPING ROADWAY(84,4)\|METHANEDIONE SEQUESTRATION(73,3)\|RESIDUAL COALBED METHANE(66,4)\|PIPELINE(60,23)\|SEQUESTERING CO OPERATIVE(58,1)\|RESIDUAL COALBED METHANE DEVELOPMENT(57,1)\|GOAF(53,22)\|RESIDUAL COALBED METHANE EXTRACTION(53,2)\|GOAF MIDDLE(52,1)\|METHANEDIONE SEQUESTRATION DOUBLE BENEFIT(51,1)\|EXTRACTION PIPE(46,10)\|ADSORBED CH4AND(46,1)\|WORKING FACE STOPING(43,4)\|WORKING FACE(39,6)\|CH4AND BROKEN COAL(38,1)\|METHANE EXTRACTION(37,1)\|SLIT GROOVE(35,2)\|BAFFLE(33,3)\|SEALING METHANEDIONE(33,2)\|CUTTING HOLE(31,3)\|RESIDUAL COALBED GAS(29,3)\|STOPING(26,4)\|BROKEN COAL ROCK(25,3)\|WORKING FACE STOPING(25,2)\|RESIDUAL COALBED GAS UTILIZATION(25,1)\|PIPE WALL(24,3)\|CLOSURE WALL(22,2)\|PIPELINE2DUE(22,1)\|DUAL BENEFIT(19,1)\|EXTRACTING(18,2)\|CO2THE GAS STORAGE TANK(17,4)\|STOPING LINE(17,4)\|CO2THE AIR STORAGE TANK(16,2)\|NONPRODUCTIVE COAL SEAMS2OUTSTANDING(13,1)\|COMPRESSIVE STRENGTH(12,3)\|WATER INJECTION(10,5)\|PUMP STATION(10,4)\|METHANEDIONE SEQUESTRATION BENEFIT(10,1)\|SEALING WALL(9,6)\|WELL DRILLING(9,6)\|AIR STORAGE TANK(9,3)\|RESIDUAL COALBED METHANE RESOURCE(9,1)\|GAS STORAGE TANK(8,6)\|AIR OUTLET(8,2)\|CO2HAS STRONG ADSORBABILITY(8,1)\|COAL PILLAR CRACK(8,1)\|ADSORBED CH4IS(7,1)\|CH4THE PROMINENCE(7,1)\|CO2FOR DISASTER(6,1)\|COAL SEAM STORE CO2CO(6,1)\|GEOLOGICAL DISPOSAL(6,1)\|MINE ROADWAY(6,1)\|VENTILATION BURDEN(6,1)\|IGNITION PHENOMENON NATURE(5,1)\|INTRODUCING CO2SEALING(5,1)\|RELEVANT SCIENTIST(5,1)\|ABANDONED RESIDUAL(4,1)\|COAL MINING RAPID DEVELOPMENT(4,1)\|COAL RESIDUE(4,1)\|DISPLACING RESIDUAL COALBED GAS(4,1)\|GLOBAL CONCERN(4,1)\|RESIDUAL DISPLACEMENT(4,1)\|STORE CO2IT(4,1)\|ADSORPTIVITY(3,1)\|ATMOSPHERE2THE(3,1)\|DUCT SLOT(3,1)\|GOAF4THE GAS EXTRACTION(3,1)\|LIVING ENVIRONMENT(3,1)\|PIPE PROTECTION(3,1)\|PRIMARY GREENHOUSE(3,1)\|SIGNIFICANCE(3,1)\|UNSAFE FACTOR(3,1)\|ADDITIVE(2,1)\|CH4AND(2,1)\|COAL ROCK MASS PAIR(2,1)\|COALBED GAS INDUSTRY(2,1)\|FACE EXTRACTION(2,1)\|FLEXIBLE PIPE(2,1)\|GLOBAL CLIMATE(2,1)\|	(CN104696005)\|1. The method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in the old goaf of the coal mine is characterized by comprising the following steps:\|a. in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) from a position 5-10 m away from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5);\|b. tightly winding a high-pressure hose (7) with the diameter of 5-15 cm and the compressive strength of 5-10 MPa on the slot (5), injecting 2-5 MPa high-pressure water into the high-pressure hose (7) when all pipelines (4) wound with the high-pressure hose (7) enter a goaf (8), and bundling a water injection port of the high-pressure hose (7) after water injection is finished;\|c. after the stoping of the working face (1) is finished, a closed wall (10) with the thickness of 2-5 m is arranged at the stoping line (9), and the pipeline (4) penetrates through the closed wall (10) and is connected to the ground (11) and the CO2A gas storage tank (12) is communicated with CO2A first valve (13) is arranged at an air outlet of the air storage tank (12);\|d. constructing a well (14) downwards from the ground (11) every 200-300 m along the middle of the goaf (8) until the bottom of the well (14) is 20-40 m away from the upper part of the goaf (8), inserting an extraction pipe (16) into the well (14) from the ground (11), and arranging a second valve (17) at the upper end of the extraction pipe (16);\|after the well mouth of the drilling well (14) is sealed, an extraction pipe (16) is connected with a pump station (15);\|e. opening a first valve (13) by CO2The gas storage tank (12) injects CO into the goaf (8) along the pipeline (4)2Simultaneously opening a second valve (17) to begin extracting CO in the goaf (8)2Displacing residual coal bed gas;\|f. when extracting CO in the pipe (16)2When the concentration is higher than 10%, the first valve (13) and the second valve (17) are closed, and the CO injection is stopped2And extracting residual coal bed gas.	(CN104696005)\|TECHNICAL FIELD\|[0002] The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction, which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf.\|BACKGROUND ART\|[0004] As global climate warms up, asCO, the main greenhouse gas2Disposal issues have become a focus of global concern to relevant scientists. To solve CO2For disasters brought to the living environment of human beings, geological disposal is well known as one of effective ways for solving the problem of influence of greenhouse gas on the environment. Wherein the deep non-recoverable coal seam stores CO2CO considered most economical2Disposal by injecting CO into the non-productive coal seam2Not only can geologically store CO2It can also be used for clean energy source-coal bed gas (CH)4) And (4) recovering.\|[0005] However, with the rapid development of coal mining technology, these non-productive coal seams will become productive in the future, and the CO brought by the non-productive coal seams2Outstanding problem will be better than CH4The prominence is more serious.\|[0006] The large-area old dead zone brought by coal mining is a natural excellent gas storage tank and is also a great risk source threatening safety production, and a large amount of high-concentration gas stored in the large-area old dead zone possibly enters a mining area or a mine roadway through a sealing wall or a coal pillar crack under the action of ventilation negative pressure and the change of atmospheric pressure, so that the ventilation burden and unsafe factors are increased. Therefore, the method is very necessary for extracting the gas in the old goaf, and if the gas is reasonably developed and utilized, the abundant high-concentration gas has extremely important significance for the development of the coal bed gas industry. At present, the gas extraction in the old goaf of the coal mine in China is not ideal, so that a method for reasonably sealing and storing CO is urgently needed2And can also improve the gas extraction rate of the goaf.\|DISCLOSURE\|[0007] Disclosure of Invention\|[0008] The invention aims to solve the problems of old goaf sealing of carbon dioxide and low extraction efficiency of residual coalbed methane in the old goaf, and provides a method for cooperatively sealing carbon dioxide in the old goaf of a coal mine to extract residual coalbed methane.\|[0009] The technical scheme of the invention is as follows: the method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in the old goaf of the coal mine comprises the following specific steps:\|[0010] a. in the working face stoping process, pipelines with the diameter of 30-50 cm are laid at the bottom of a stoping roadway from a position 5-10 m away from a cutting hole, 4 slots which are axially parallel to the pipelines and symmetrically distributed are arranged on the pipe wall of each pipeline every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles with the height of 15-25 cm are arranged at two ends of each slot.\|[0011] b. And tightly winding a high-pressure hose with the diameter of 5-15 cm and the compressive strength of 5-10 MPa on the slot. When all the pipelines wound with the high-pressure hoses enter a mining area, 2-5 MPa of high-pressure water is injected into the high-pressure hoses, and a water injection port of the high-pressure hoses is bound after water injection is finished.\|[0012] c. And after the stoping of the working face is finished, a sealing wall with the thickness of 2-5 m is arranged at the stoping line. The pipeline passes through the sealed wall and is connected to the ground and CO2The gas storage tank is communicated, and a gas outlet of the gas storage tank is provided with a first valve.\|[0013] d. And (3) drilling a well downwards from the ground every 200-300 m along the middle part of the goaf until the bottom of the drilling well is 20-40 m away from the upper part of the goaf, inserting an extraction pipe into the drilling well from the ground, and arranging a second valve at the upper end of the extraction pipe. And after the well mouth of the well is sealed, the extraction pipe is connected with a pump station.\|[0014] e. Opening a first valve by CO2The gas storage tank injects CO into the goaf along the pipeline2. Simultaneously opening a second valve to begin extracting CO in the goaf2And (4) displacing residual coal bed gas.\|[0015] f. When extracting CO in the pipe2When the concentration is higher than 10%, the first valve and the second valve are closed, and CO injection is stopped2And extracting residual coal bed gas.\|[0016] The invention has the beneficial effects that:\|[0017] (1) the high-pressure flexible pipe protection technology is adopted, water with certain pressure is injected into the flexible pipe, so that the pipeline is protected in a pressure yielding mode, and the broken coal rocks are prevented from damaging the pipeline and blocking air holes;\|[0018] (2) by using CO2Density ofGreater than CH4And crushing coal rock mass pair CO at the top of the goaf2The characteristic of greater adsorptivity, in injecting CO into the goaf2In the process of (A), CO2Firstly occupying the space at the lower part of the goaf and crushing the original adsorbed CH of the coal rock mass4Is displaced and gradually moves upwards to the top of the goaf for accumulation, and then the drilling well is used for drilling CH in the goaf4The gas extraction efficiency of the goaf is greatly improved by extraction;\|[0019] (3) introducing CO2Sealing and storing the waste gas in the old goaf of the coal mine, thereby not only reducing the emission of CO to the atmosphere2The amount of the additive is reduced, the greenhouse effect is relieved, the natural ignition phenomenon of the residual coal in the old goaf can be effectively inhibited, and the safety of a mine is enhanced;\|[0020] (4) the originally abandoned residual coalbed methane resources in the goaf are developed and utilized, and the method has double benefits of carbon dioxide sequestration and development and utilization of the residual coalbed methane resources.\|DRAWINGS DESCRIPTION\|[0022] FIG. 1 is a schematic view of a pipeline laid during the face extraction process\|[0023] FIG. 2 is a schematic diagram of the principle of the present invention\|[0024] FIG. 3 is a schematic view of a duct slot\|[0025] FIG. 4 is a cross-sectional view taken along line A-A in FIG. 3\|[0026] In the figure: 1-working face, 2-cutting hole, 3-mining roadway, 4-pipeline, 5-slot,\|[0027] 6-baffle, 7-high pressure hose, 8-goaf, 9-stoping line, 10-sealing wall,\|[0028] 11-ground, 12-CO2Gas storage tank, 13-first valve, 14-drilling well, 15-pump station,\|[0029] 16-an extraction pipe, 17-a second valve.\|INVENTION MODE\|[0030] Detailed Description\|[0031] Examples of the invention are further described below with reference to the accompanying drawings:\|[0032] the invention discloses a method for cooperatively sealing carbon dioxide and developing residual coalbed methane in a coal mine goaf, which comprises the following steps: in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) at a distance of 5-10 m from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5). And a high-pressure hose (7) with the diameter of 5-15 cm and the compressive strength of 5-10 MPa is tightly wound on the slot (5). When the pipeline (4) wound with the high-pressure hose (7) completely enters the goaf (8), 2-5 MPa of high-pressure water is injected into the high-pressure hose (7), the pipeline (4) is protected in a yielding manner, the pipeline (4) is prevented from being damaged by broken coal rocks and blocking air holes, and the high-pressure hose (7) is bound after the water injection is finished. After the stoping of the working face (1) is finished, a sealing wall (10) with the thickness of 2-5 m is arranged at the stoping line (9). The pipeline (4) passes through the sealed wall (10) and is connected to the ground (11) and CO2The air storage tank (12) is communicated, and a first valve (13) is arranged at an air outlet of the air storage tank (12). And (3) constructing a well (14) downwards from the ground (11) every 200-300 m along the middle part of the goaf (8) until the bottom of the well (14) is 20-40 m away from the upper part of the goaf (8), inserting an extraction pipe (16) into the well (14) from the ground, and arranging a second valve (17) on the extraction pipe (16). After the well mouth of the drilling well (14) is sealed, the extraction pipe (16) is connected with a pump station (15). Opening the first valve (13) by CO2The gas storage tank (12) injects CO2 into the gob (8) along the pipeline (4). During injection, due to CO2Density greater than CH4,CO2Firstly occupying the space at the lower part of the goaf (8), and crushing coal rocks at the top of the goaf (8) to CO2Has stronger adsorbability, namely the original adsorbed CH4Is displaced and gradually moves upwards to the top of the goaf (8) for accumulation. And opening a second valve (17) to begin extracting residual coal bed gas in the goaf (8). When extracting CO in the pipe (16)2When the concentration is higher than 10%, the first valve (13) and the second valve (17) are closed, and the CO injection is stopped2And extracting residual coal bed gas.	(CN104696005)\|TECHNICAL FIELD\|[0002] The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction, which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf.\|BACKGROUND ART\|[0004] As global climate warms up, asCO, the main greenhouse gas2Disposal issues have become a focus of global concern to relevant scientists. To solve CO2For disasters brought to the living environment of human beings, geological disposal is well known as one of effective ways for solving the problem of influence of greenhouse gas on the environment. Wherein the deep non-recoverable coal seam stores CO2CO considered most economical2Disposal by injecting CO into the non-productive coal seam2Not only can geologically store CO2It can also be used for clean energy source-coal bed gas (CH)4) And (4) recovering.\|[0005] However, with the rapid development of coal mining technology, these non-productive coal seams will become productive in the future, and the CO brought by the non-productive coal seams2Outstanding problem will be better than CH4The prominence is more serious.\|[0006] The large-area old dead zone brought by coal mining is a natural excellent gas storage tank and is also a great risk source threatening safety production, and a large amount of high-concentration gas stored in the large-area old dead zone possibly enters a mining area or a mine roadway through a sealing wall or a coal pillar crack under the action of ventilation negative pressure and the change of atmospheric pressure, so that the ventilation burden and unsafe factors are increased. Therefore, the method is very necessary for extracting the gas in the old goaf, and if the gas is reasonably developed and utilized, the abundant high-concentration gas has extremely important significance for the development of the coal bed gas industry. At present, the gas extraction in the old goaf of the coal mine in China is not ideal, so that a method for reasonably sealing and storing CO is urgently needed2And can also improve the gas extraction rate of the goaf.\|DISCLOSURE\|[0007] Disclosure of Invention\|[0008] The invention aims to solve the problems of old goaf sealing of carbon dioxide and low extraction efficiency of residual coalbed methane in the old goaf, and provides a method for cooperatively sealing carbon dioxide in the old goaf of a coal mine to extract residual coalbed methane.\|[0009] The technical scheme of the invention is as follows: the method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in the old goaf of the coal mine comprises the following specific steps:\|[0010] a. in the working face stoping process, pipelines with the diameter of 30-50 cm are laid at the bottom of a stoping roadway from a position 5-10 m away from a cutting hole, 4 slots which are axially parallel to the pipelines and symmetrically distributed are arranged on the pipe wall of each pipeline every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles with the height of 15-25 cm are arranged at two ends of each slot.\|[0011] b. And tightly winding a high-pressure hose with the diameter of 5-15 cm and the compressive strength of 5-10 MPa on the slot. When all the pipelines wound with the high-pressure hoses enter a mining area, 2-5 MPa of high-pressure water is injected into the high-pressure hoses, and a water injection port of the high-pressure hoses is bound after water injection is finished.\|[0012] c. And after the stoping of the working face is finished, a sealing wall with the thickness of 2-5 m is arranged at the stoping line. The pipeline passes through the sealed wall and is connected to the ground and CO2The gas storage tank is communicated, and a gas outlet of the gas storage tank is provided with a first valve.\|[0013] d. And (3) drilling a well downwards from the ground every 200-300 m along the middle part of the goaf until the bottom of the drilling well is 20-40 m away from the upper part of the goaf, inserting an extraction pipe into the drilling well from the ground, and arranging a second valve at the upper end of the extraction pipe. And after the well mouth of the well is sealed, the extraction pipe is connected with a pump station.\|[0014] e. Opening a first valve by CO2The gas storage tank injects CO into the goaf along the pipeline2. Simultaneously opening a second valve to begin extracting CO in the goaf2And (4) displacing residual coal bed gas.\|[0015] f. When extracting CO in the pipe2When the concentration is higher than 10%, the first valve and the second valve are closed, and CO injection is stopped2And extracting residual coal bed gas.\|[0016] The invention has the beneficial effects that:\|[0017] (1) the high-pressure flexible pipe protection technology is adopted, water with certain pressure is injected into the flexible pipe, so that the pipeline is protected in a pressure yielding mode, and the broken coal rocks are prevented from damaging the pipeline and blocking air holes;\|[0018] (2) by using CO2Density ofGreater than CH4And crushing coal rock mass pair CO at the top of the goaf2The characteristic of greater adsorptivity, in injecting CO into the goaf2In the process of (A), CO2Firstly occupying the space at the lower part of the goaf and crushing the original adsorbed CH of the coal rock mass4Is displaced and gradually moves upwards to the top of the goaf for accumulation, and then the drilling well is used for drilling CH in the goaf4The gas extraction efficiency of the goaf is greatly improved by extraction;\|[0019] (3) introducing CO2Sealing and storing the waste gas in the old goaf of the coal mine, thereby not only reducing the emission of CO to the atmosphere2The amount of the additive is reduced, the greenhouse effect is relieved, the natural ignition phenomenon of the residual coal in the old goaf can be effectively inhibited, and the safety of a mine is enhanced;\|[0020] (4) the originally abandoned residual coalbed methane resources in the goaf are developed and utilized, and the method has double benefits of carbon dioxide sequestration and development and utilization of the residual coalbed methane resources.\|DRAWINGS DESCRIPTION\|[0022] FIG. 1 is a schematic view of a pipeline laid during the face extraction process\|[0023] FIG. 2 is a schematic diagram of the principle of the present invention\|[0024] FIG. 3 is a schematic view of a duct slot\|[0025] FIG. 4 is a cross-sectional view taken along line A-A in FIG. 3\|[0026] In the figure: 1-working face, 2-cutting hole, 3-mining roadway, 4-pipeline, 5-slot,\|[0027] 6-baffle, 7-high pressure hose, 8-goaf, 9-stoping line, 10-sealing wall,\|[0028] 11-ground, 12-CO2Gas storage tank, 13-first valve, 14-drilling well, 15-pump station,\|[0029] 16-an extraction pipe, 17-a second valve.\|INVENTION MODE\|[0030] Detailed Description\|[0031] Examples of the invention are further described below with reference to the accompanying drawings:\|[0032] the invention discloses a method for cooperatively sealing carbon dioxide and developing residual coalbed methane in a coal mine goaf, which comprises the following steps: in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) at a distance of 5-10 m from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5). And a high-pressure hose (7) with the diameter of 5-15 cm and the compressive strength of 5-10 MPa is tightly wound on the slot (5). When the pipeline (4) wound with the high-pressure hose (7) completely enters the goaf (8), 2-5 MPa of high-pressure water is injected into the high-pressure hose (7), the pipeline (4) is protected in a yielding manner, the pipeline (4) is prevented from being damaged by broken coal rocks and blocking air holes, and the high-pressure hose (7) is bound after the water injection is finished. After the stoping of the working face (1) is finished, a sealing wall (10) with the thickness of 2-5 m is arranged at the stoping line (9). The pipeline (4) passes through the sealed wall (10) and is connected to the ground (11) and CO2The air storage tank (12) is communicated, and a first valve (13) is arranged at an air outlet of the air storage tank (12). And (3) constructing a well (14) downwards from the ground (11) every 200-300 m along the middle part of the goaf (8) until the bottom of the well (14) is 20-40 m away from the upper part of the goaf (8), inserting an extraction pipe (16) into the well (14) from the ground, and arranging a second valve (17) on the extraction pipe (16). After the well mouth of the drilling well (14) is sealed, the extraction pipe (16) is connected with a pump station (15). Opening the first valve (13) by CO2The gas storage tank (12) injects CO2 into the gob (8) along the pipeline (4). During injection, due to CO2Density greater than CH4,CO2Firstly occupying the space at the lower part of the goaf (8), and crushing coal rocks at the top of the goaf (8) to CO2Has stronger adsorbability, namely the original adsorbed CH4Is displaced and gradually moves upwards to the top of the goaf (8) for accumulation. And opening a second valve (17) to begin extracting residual coal bed gas in the goaf (8). When extracting CO in the pipe (16)2When the concentration is higher than 10%, the first valve (13) and the second valve (17) are closed, and the CO injection is stopped2And extracting residual coal bed gas.	Family Number\|(69557757)\|69557757\|Object of Invention\|(CN104696005B B)\|The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction , which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf . \|(CN104696005 A)\|The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction , which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf . \|Abstract\|(CN104696005B B)\|The invention discloses a method for synchronously extracting residual coalbed methane and sealing and preserving carbon dioxide in an old coal mined - out area of coal mine . The method comprises the following steps : during working face mining , a pipeline is paved at the bottom of a mining roadway , seam grooves are axially formed in the pipeline at intervals , baffles are arranged on both ends of each seam groove , high - pressure hoses are respectively wound on the seam grooves , water under a certain pressure is injected in the high - pressure hoses to perform & apos ; yielding&apos ; protection on the pipeline , so that crushed coal and rock in the mined - out area can be prevented from destroying the pipeline and blocking air holes ; after working face mining is finished , a fire dam is arranged at a mining stop line , the pipeline is communicated to the ground , and well drilling is constructed from the ground to the upper part of the mined - out area ; CO2 is injected from the ground to the mined out area along the pipeline , because the density of the CO2 is larger than CH4 , and the crushed coal and rock remained at the bottom of the mined - out area has higher adsorptivity to CO2 , the absorbed CH4 is replaced out and is accumulated at the top of the mined - out area , and the accumulated CH4 is extracted by well drilling . The method has dual benefits of sealing and preserving the carbon dioxide , and developing and utilizing the residual coalbed methane . \|	Civil engineering	E21B-041/00/64\|E21B-043/00/6\|E21B-043/16/4\|E21F-007/00\|Y02P-090/70		E21B-041/00/64\|E21B-043/00/6\|E21B-043/16/4\|E21F-007/00\|Y02P-090/70	E21B-043/16\|E21F-007/00	E21B-043/16\|E21F-007/00			CN112943347\|CN110608022\|CN109488269B\|CN119145824B\|CN116575900B\|CN115492557B\|CN113027511B\|CN105797570B	CN112943347 94683113 WHO=Examiner SELF=Y CAT=A\|CN110608022 87065712 WHO=Examiner SELF=N CAT=A\|CN109488269B 83753115 WHO=Examiner SELF=N CAT=A\|CN119145824B 112657834 WHO=Examiner SELF=N\|CN116575900B 106093745 WHO=Examiner SELF=Y\|CN115492557B 103072638 WHO=Examiner SELF=N\|CN113027511B 101827199 WHO=Examiner SELF=N\|CN105797570B 73701055 WHO=Examiner SELF=N	CN102877819\|CN103670338\|CN102587958\|CN102226412\|RU2445462\|CN101418679	CN102877819 8051501 WHO=Examiner SELF=N CAT=A\|CN103670338 64988101 WHO=Examiner SELF=N CAT=A\|CN102587958 7811393 WHO=Examiner SELF=N CAT=A\|CN102226412 7462754 WHO=Examiner SELF=N CAT=A\|RU2445462 36341417 WHO=Examiner SELF=N CAT=A\|CN101418679 6743135 WHO=Examiner SELF=Y CAT=A		CN101418679; CN102226412; RU2445462; CN102587958; CN102877819; CN103670338		GRANTED	(CN104696005)\|GRANTED	ALIVE	(CN104696005)\|ALIVE	(CN104696005)\|LEGAL DETAILS FOR CN104696005\|Actual or expected expiration date=2035-02-03\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-02-03\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201510055353\|Application date=2015-02-03\|Standardized application number=2015CN-0055353\|Event publication date=2015-06-10\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN104696005\|Publication stage code=A\|Publication date=2015-06-10\|Standardized publication number=CN104696005\|Event publication date=2015-06-10\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2015-07-08\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2016-08-31\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN104696005\|Publication stage code=B\|Publication date=2016-08-31\|Standardized publication number=CN104696005B\|Event publication date=2016-08-31\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right		(CN104696005)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjmjLykQKxGtiRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000013731776&ekey=2330&xpn=CN104696005B&kind=B	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=eoY4Iua8XF2Kfx%252FE0Z3k1rmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN104696005)\|CN	(CN104696005)\|NAME=TAIYUAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN		(CN104696005)\|NAME=LU MAOCHUN;KERUIDA PATENT AGENCY CO., LTD. TAIYUAN CITY , REG=14101\|(CN104696005)\|NAME=LU MAOCHUN;KERUIDA PATENT AGENCY CO., LTD. TAIYUAN CITY		(CN104696005)\|NAME=HU SHENGYONG\|NAME=GAO QIANG\|NAME=CHEN CHUNJIAN\|NAME=ZHANG XIANG\|(CN104696005)\|NAME=HU SHENGYONG\|NAME=GAO QIANG\|NAME=CHEN CHUNJIAN\|NAME=ZHANG XIANG	(CN104696005)\|4	1	1					(CN104696005)\|Number of Claims: NCL=1\|Gazette date: GAZDATE=2016-08-31\|Gazette number: GAZNUM=32-35\|Number of Pages: NPAGES=7\|Primary examiner: 隗敏\|Primary examiner: Kui Min\|\|(CN104696005)\|Number of Claims: NCL=1\|Gazette date: GAZDATE=2015-06-10\|Gazette number: GAZNUM=31-24\|Number of Pages: NPAGES=7\|Primary examiner: 隗敏\|Primary examiner: Kui Min\|		(CN104696005)\|CHINESE (CHI)	(CN104696005B)\|Patent\|(CN104696005)\|Patent	Titre: (CN104696005)\|Method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in old goaf of coal mine Résumé: (CN104696005)\|The invention discloses a method for synchronously extracting residual coalbed methane and sealing and preserving carbon dioxide in an old coal mined-out area of coal mine. The method comprises the following steps: during working face mining, a pipeline is paved at the bottom of a mining roadway, seam grooves are axially formed in the pipeline at intervals, baffles are arranged on both ends of each seam groove, high-pressure hoses are respectively wound on the seam grooves, water under a certain pressure is injected in the high-pressure hoses to perform 'yielding' protection on the pipeline, so that crushed coal and rock in the mined-out area can be prevented from destroying the pipeline and blocking air holes; after working face mining is finished, a fire dam is arranged at a mining stop line, the pipeline is communicated to the ground, and well drilling is constructed from the ground to the upper part of the mined-out area; CO2 is injected from the ground to the mined out area along the pipeline, because the density of the CO2 is larger than CH4, and the crushed coal and rock remained at the bottom of the mined-out area has higher adsorptivity to CO2, the absorbed CH4 is replaced out and is accumulated at the top of the mined-out area, and the accumulated CH4 is extracted by well drilling. The method has dual benefits of sealing and preserving the carbon dioxide, and developing and utilizing the residual coalbed methane.	33	Abstract	gpt-4o-mini	no	The article focuses on extracting methane and sealing carbon dioxide in a mined area, without addressing the accelerated weathering of minerals or carbon sequestration through mineral alteration.
36	CN202110837467	CN202110837467	CN113494265\|CN113494265	96423759	CN113494265 B 2023-05-02 [CN113494265B]\|CN113494265 A 2021-10-12 [CN113494265]	2021-07-23	2021-07-23	2023-05-02\|2021-10-12	(CN113494265B)\|2023-05-02	(CN113494265)\|2025-07-18	(CN113494265)\|Plugging method for leakage along abandoned well in carbon dioxide geological storage process	(CN113494265)\|The invention provides a method for blocking leakage along an abandoned well in the geological storage process of carbon dioxide. The method comprises the following steps that perforating is carried out by adopting a stable cover layer above a geological storage layer of carbon dioxide; a shaft with leakage risk, drilling annular cement and a surrounding rock fracture zone communicate with one another; and lime milk turbid liquid is injected into a perforation interval, so that lime milk in a gap reacts with leaked carbon dioxide to form hardened and compact calcium carbonate, and a carbon dioxide leakage channel is blocked. According to the method for blocking leakage along the abandoned well in the geological storage process of carbon dioxide, the crack channel leaking along the abandoned well in the geological storage process of carbon dioxide can be effectively blocked, meanwhile, a surrounding rock broken zone and crack-containing drilling well annulus cement can be cemented into a compact whole, and the risk of leaking along the abandoned well in the geological storage process of carbon dioxide is greatly reduced. The injected lime milk turbid liquid reacts with carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, the geological environment pollution risk is extremely low, and the plugging process is safe and environmentally friendly.	CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS	(CN113494265)\|CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS ([CN])\|(CN113494265)\|CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS ([CN])	FU LEI\|MA XIN\|DIAO YUJIE\|ZHANG CHENGLONG\|LIU TING\|Fu Jie\|SHAO WEI	(CN113494265)\|FU LEI\|MA XIN\|DIAO YUJIE\|ZHANG CHENGLONG\|LIU TING\|Fu Jie\|SHAO WEI\|(CN113494265)\|FU LEI\|MA XIN\|DIAO YUJIE\|ZHANG CHENGLONG\|LIU TING\|Fu Jie\|SHAO WEI	(CN113494265)\|CHEN YING;BEIJING BEIXIN-ZHICHENG INTELLECTUAL PROPERTY AGENT CO., LTD.\|Reg. Nb: 11100	(CN113494265)\|At present, great project demonstration of carbon capture utilization and sealing is developed in each industry of China, and a foundation is laid for subsequent large-scale carbon dioxide injection.\|It is also a good measure that the perforation segments are evenly distributed over the entire circumference of the inner wall of the well.\|According to the invention, lime milk is injected into the perforation of the cover layer, and on annular cement and surrounding rock fracture zones where cracks appear due to the damage of drilling on the cover layer, the lime milk and carbon dioxide meet and react in the cracks to generate calcium carbonate to fill and seal the cracks, so that the cover layer is repaired.\|However, if the initial set concentration is too high, the lime milk is too thick, and besides the problems of the above and the increase of the concentration reduction times, ports of some cracks are sealed by the thick lime milk, so that the whole annular cement and the size cracks in the surrounding rock breaking zone are not filled, and the sealing effect is also affected.\|The injection rate described above also affects the occlusion effect.\|	(CN113494265)\|1. A plugging method for leakage along an abandoned well in a carbon dioxide geological storage process is characterized by comprising the following steps of: the method comprises the following steps:step 1: perforating, namely perforating a perforating section formed on the inner wall of the shaft corresponding to the thickness of the stable covering layer, and communicating the annular cement of the drilling well with cracks of the surrounding rock breaking zone;step 2: injecting lime milk suspension, namely injecting the lime milk suspension into the perforation, so that the lime milk suspension enters the crack and reacts with leaked carbon dioxide to form calcium carbonate, and further plugging a leakage channel of the carbon dioxide;the plugging method further comprises at least one of the following steps:prior to step 1, comprising:a leakage identification step of identifying whether or not the abandoned well has carbon dioxide leaked along the well; and/or the number of the groups of groups,cleaning the inside of the well, namely cleaning a sealing bridge plug in the well before sealing the leaked abandoned well, and ensuring the smoothness and smoothness of the inner wall of the well shaft above the carbon dioxide geological sealing storage layer;and/or the number of the groups of groups,after step 2, it includes:a plugging effect monitoring step, namely monitoring the plugging effect of the well drilling after plugging; and/or, well sealing, namely, sealing the well by an in-well bridge plug for the well drilling after the well is plugged;in the step (1) of the process,before perforation, a relatively closed space is arranged in the well corresponding to the cover layer part, and the perforation section is arranged in the space; and/or the number of the groups of groups,in the step 2 of the process, the process is carried out,injecting lime milk suspension through a fracturing truck; and/or when injection begins, the injection pressure P is less than the reservoir pressure P 0 When the concentration of the lime milk suspension is an initial set concentration, and when P is larger than P 0 When the concentration of the lime milk suspension is reduced at a threshold value, the lime milk suspension is continuously injected, and when P is larger than P again 0 And when the threshold value is reached, the concentration of the lime milk suspension is reduced again, then the injection is continued until the concentration of the lime milk suspension is equal to a final set concentration, namely, the injection is continued at the final set concentration until the injection pressure P reaches an injection termination set pressure, and the injection is ended.\|	(CN113494265)\|The invention provides a maximum rate limit of 0.5 liter/second at which lime milk entering the crack can react with leaked carbon dioxide in good time to form calcium carbonate to seal the crack.\|The invention provides a plugging method for leakage along an abandoned well in a carbon dioxide geological storage process, which comprises the steps of perforating a stable cover layer on a carbon dioxide geological storage layer, communicating a shaft with leakage risk, drilling annular cement and a surrounding rock breaking belt, injecting lime milk suspension into a perforation section, enabling lime milk in a gap to react with leaked carbon dioxide to form hardened and compact calcium carbonate, and plugging a carbon dioxide leakage channel.\|	(CN113494265)\|CARBON DIOXIDE(100,110)\|LIME MILK SUSPENSION(100,57)\|PLUGGING(100,38)\|WELL ABANDONMENT(100,30)\|LEAKAGE(100,12)\|GEOLOGICAL STORAGE(100,3)\|CARBON DIOXIDE GEOLOGICAL STORAGE(100,1)\|GEOLOGICAL STORAGE(100,1)\|ANNULAR CEMENT(48,12)\|ROCK BREAKING ZONE(47,8)\|ANTILEAKAGE BRIDGE PLUGIN(44,1)\|DRILLING ANNULUS PERMEABILITY(40,1)\|SEALING BRIDGE PLUGIN(39,2)\|PLUGGING BRIDGE PLUGIN(37,1)\|PERFORATION SEGMENT(33,1)\|PERFORATING SECTION(32,27)\|LEAKAGE IDENTIFICATION(32,4)\|FRACTURING TRUCK(30,4)\|CARBON CAPTURE UTILIZATION DEMONSTRATION(30,1)\|CRACK(29,21)\|CORROSION RESISTANT CEMENT(29,6)\|INJECTED LIME MILK SUSPENSION(29,5)\|CRACK PORT(29,1)\|PERFORATION(27,20)\|ABANDONED BOREHOLE SONIC LOGGING(27,2)\|DRILLING DAMAGE(27,1)\|GEOLOGICAL ENVIRONMENT POLLUTION(26,3)\|THICK LIME MILK(26,1)\|LIME MILK(25,26)\|COVER LAYER(24,34)\|GEOLOGICAL SEALING(24,5)\|SMOOTHNESS(24,4)\|DRILLING ANNULAR CEMENT(24,2)\|POZZOLAN CEMENT(23,2)\|ROCK FRACTURE ZONE(22,8)\|BRIDGE PLUG(22,2)\|OVERLYING STRATUM(22,2)\|CALCIUM CARBONATE(21,15)\|PACKER INSTALLATION(21,2)\|CARBON DIOXIDE GEOLOGICAL SEALING(20,3)\|ANALYZING LOGGING(20,2)\|BRIDGE PLUG IN(20,2)\|RESERVOIR(19,16)\|GEOLOGICAL STORAGE LAYER(19,2)\|LIME MILK SUSPENSION INJECTION(18,3)\|FOUNDATION(18,1)\|PIPE ORIFICE(18,1)\|UTILIZING CARBON CAPTURE(18,1)\|FULL CIRCUMFERENCE(17,1)\|INJECTION PRESSURE(16,16)\|UPPER PACKER(16,8)\|CEMENT COMPOSITE(16,3)\|FLY ASH CEMENT(16,3)\|WELLHEAD PERIMETER CARBON DIOXIDE(16,3)\|CAP LAYER(15,15)\|CRACK CHANNEL(15,3)\|CARBON DIOXIDE INJECTION(15,1)\|CARBON DIOXIDE MEET(15,1)\|CALCIUM HYDROXIDE SOLUBILITY(14,2)\|SIZE CRACK(14,1)\|LEAKAGE RISK(13,8)\|PACKER DISTANCE(13,7)\|DRILLING ANNULUS CEMENT(12,3)\|DRILLING WELL ANNULAR CEMENT(12,2)\|INJECTION PIPE(11,7)\|LEAKAGE CHANNEL(11,6)\|COMPACT WHOLE(11,5)\|LIME MILK SUSPENSION SET(11,4)\|STABLE COVERING LAYER(11,4)\|INJECTION RATE(11,2)\|INJECTION SPEED(11,1)\|LIME MILK SATURATED SOLUTION(11,1)\|THRESHOLD VALUE(10,17)\|ROCK(10,4)\|CORRELATION(10,2)\|LEAKED ABANDONED WELL(10,2)\|LOGGING DATA(10,2)\|MONITORING PERIOD(10,2)\|RESERVOIR LAYER(10,2)\|CARBON DIOXIDE LEAKAGE PATH(10,1)\|FINAL SET(9,11)\|STABLE COVER LAYER(9,5)\|PERFORATED SECTION(9,4)\|STABLE COVERING LAYER THICKNESS(9,4)\|STORAGE LAYER(9,4)\|MONITORING FREQUENCY(9,3)\|SLAG CEMENT(9,3)\|CARBON DIOXIDE(9,1)\|WELL DRILLING(8,11)\|INJECTION TERMINATION SETTING PRESSURE(8,2)\|PH VALUE PROBE(8,2)\|RESERVOIR PRESSURE(8,2)\|EVENLY DISTRIBUTED OVER(8,1)\|UPPER EDGE(7,9)\|PRESSURE DIFFERENCE(7,5)\|CARBON DIOXIDE LEAKAGE CHANNEL(7,4)\|CONSTANT VALUE(7,4)\|LEAK IDENTIFICATION(7,4)\|BLOWOUT PREVENTION PROTECTION DEVICE(7,3)\|CARBON DIOXIDE RESERVOIR TEMPERATURE(7,2)\|DRILLING MACHINE(7,2)\|BOREHOLE ANNULUS CEMENT(7,1)\|CEMENT BRIDGE PLUGIN(7,1)\|OCCLUSION EFFECT(7,1)\|INNER WALL(6,9)\|PERFORATING SECTION HEIGHT(6,7)\|FORMATION TEMPERATURE(6,5)\|CARBON DIOXIDE SEALING(6,4)\|EXHAUST VALVE(6,4)\|SAFE(6,3)\|CARBON DIOXIDE GEOLOGICAL SEQUESTRATION(6,2)\|CEMENT SHEATH(6,2)\|OVERBURDEN STRATUM(6,1)\|OVERBURDEN WEAKNESS(6,1)\|WELL SHAFT(5,7)\|INJECTION TERMINATION SET PRESSURE(5,4)\|FINE CRACK(5,3)\|ABANDONED DRILLING WELL(5,2)\|CIRCUMFERENTIAL SURFACE(5,2)\|PLUGGING LEAKAGE(5,2)\|ANNULUS PERMEABILITY(5,1)\|CALCULATED STRATUM PERMEABILITY(5,1)\|LEAKAGE PROOF BRIDGE PLUGIN(5,1)\|MAXIMUM RATE LIMIT(5,1)\|WELLBORE BRIDGE PLUG(5,1)\|WELLHEAD GAS FLOWMETER(5,1)\|WELLHEAD VENT VALVE(5,1)\|WELL SEALING(4,4)\|CARBON NEUTRALIZATION(4,2)\|STIRRING BOX(4,2)\|MONITORING PLUGGING(4,1)\|REPAIRING DIFFICULTY(4,1)\|VOLCANIC ASH CEMENT(4,1)\|CONCENTRATION REDUCTION TIME(3,2)\|CONTINUITY(3,2)\|FORMATION WATER(3,2)\|LAYER PROTECTION(3,2)\|ABANDONED HYDROCARBON RESERVOIR(3,1)\|ABANDONED WELLBORE(3,1)\|BLOWOUT PREVENTER COMPONENT(3,1)\|CLAY CONTENT(3,1)\|FOSSIL ENERGY(3,1)\|GEOLOGICAL SEAL STORAGE(3,1)\|GREENHOUSE GAS GEOLOGICAL SEALING(3,1)\|HARDENED COMPACT CALCIUM CARBONATE(3,1)\|IDENTIFYING LEAKAGE(3,1)\|INJECTING LIME MILK(3,1)\|LEAKAGE REASON(3,1)\|LEAKAGE SEALING(3,1)\|LIME MILK REACTION(3,1)\|LIME MILK SUSPENSION REACTION(3,1)\|LIME SUSPENSION(3,1)\|OVERLYING STRATUM WATER(3,1)\|PERFORATION INTERVAL(3,1)\|SUDDEN LEAKAGE(3,1)\|\|(CN113494265)\|CARBON DIOXIDE(100,110)\|LIME MILK SUSPENSION(100,55)\|WELL ABANDONMENT(100,24)\|BLOCKING LEAKAGE(100,4)\|CARBON DIOXIDE SEQUESTRATION(100,4)\|CARBON DIOXIDE SEQUESTRATION(100,3)\|SEQUESTRATION(100,3)\|PLUGGING LEAKAGE(100,1)\|ROCK CRUSHING ZONE(59,1)\|DRILLING ANNULAR CEMENT(43,2)\|INJECTING LIME MILK(38,8)\|DRILLING ANNULUS PERMEABILITY(38,2)\|PLUGGING(37,34)\|ANNULAR CEMENT(36,12)\|BLOCKING BRIDGE PLUGIN(36,1)\|PLUGGING BRIDGE PLUGIN(34,3)\|LEAK PROOF BRIDGE PLUGIN(34,1)\|PERFORATION(33,22)\|ROCK FRACTURE ZONE(33,15)\|CORROSION RESISTANT CEMENT(33,6)\|BRIDGE PLUG IN(33,4)\|OVERBURDEN STRATUM(32,2)\|SUDDEN LEAKAGE(32,1)\|ABANDONED BOREHOLE SONIC LOGGING(31,2)\|PERFORATION SEGMENT(31,2)\|GEOLOGICAL ENVIRONMENT POLLUTION(29,3)\|PERFORATING SECTION(28,26)\|LEAKAGE IDENTIFICATION(28,4)\|HARDENED COMPACT CALCIUM CARBONATE(28,3)\|GEOLOGICAL STORAGE LAYER(28,1)\|GEOLOGICAL SEALING(27,6)\|HARDENED COMPACT(26,3)\|POZZOLAN CEMENT(26,2)\|LIME MILK SUSPENSION SETTING(26,1)\|CEMENT INJECTION(25,1)\|LIME MILK(24,28)\|CALCIUM CARBONATE(24,15)\|FRACTURING TRUCK(24,6)\|UNSATURATED LIME WATER INJECTION(24,1)\|CRACK(23,15)\|ANALYZING LOGGING(23,2)\|WELLHEAD PERIPHERY(22,3)\|LIME MILK SUSPENSION INJECTION(22,2)\|UPPER PACKER(19,8)\|FLY ASH CEMENT(19,3)\|FULL CIRCUMFERENCE(19,1)\|INJECTION PRESSURE(18,17)\|CEMENT COMPOSITE(18,3)\|ROCK BREAKING ZONE(18,3)\|PERFORATED SECTION(18,2)\|UNSATURATED LIME WATER(18,1)\|STABLE COVER LAYER(17,10)\|CARBON DIOXIDE LEAKAGE(17,8)\|CRACK CHANNEL(17,3)\|GEOLOGICAL STORAGE(17,1)\|CAP LAYER(16,7)\|LEAKAGE RISK(16,5)\|CALCIUM HYDROXIDE SOLUBILITY(16,2)\|INJECTION RATE(16,1)\|P0AND P0THE PRESSURE DIFFERENCE(15,2)\|ENVIRONMENTAL PROTECTION(15,1)\|LEAKAGE CHANNEL(14,5)\|FRACTURE(13,7)\|CIRCULATING MODE(13,2)\|LIME MILK SATURATED SOLUTION(13,1)\|INJECTION PIPE(12,7)\|WHOLE SEAL(12,3)\|THRESHOLD VALUE(11,17)\|DRILLING ANNULUS CEMENT(11,2)\|MONITORING PERIOD(11,2)\|P0WHEN(11,2)\|FINAL SET(10,11)\|STABLE COVER LAYER THICKNESS(10,5)\|MONITORING FREQUENCY(10,3)\|SLAG CEMENT(10,3)\|INJECTION SPEED(10,2)\|RESERVOIR PRESSURE(10,2)\|SOLUTION LEVEL(10,1)\|CARBON DIOXIDE LEAKAGE CHANNEL(9,3)\|PH VALUE PROBE(9,3)\|ANTILEAKAGE BRIDGE PLUGIN(9,1)\|EVENLY DISTRIBUTED OVER(9,1)\|UPPER EDGE(8,9)\|CONSTANT VALUE(8,4)\|LEAK IDENTIFICATION(8,4)\|PLUGGED WELL(8,4)\|PLUGGING(8,4)\|BLOWOUT PREVENTION PROTECTION DEVICE(8,2)\|CARBON DIOXIDE RESERVOIR TEMPERATURE(8,2)\|DRILLING MACHINE(8,2)\|CEMENT BRIDGE PLUGIN(8,1)\|LIME MILKTHE SUSPENSION(8,1)\|WELL ROCK FRACTURE ZONE(8,1)\|EXHAUST VALVE(7,4)\|SAFE(7,3)\|CEMENT SHEATH(7,2)\|RESERVOIR STRATUM(7,2)\|GREENHOUSE GAS GEOLOGICAL SEQUESTRATION(7,1)\|PLUGGING ABANDONED BOREHOLE(7,1)\|INNER WALL(6,9)\|WELLBORE(6,5)\|ARGILLACEOUS CONTENT(6,2)\|CIRCUMFERENTIAL SURFACE(6,2)\|LIME MILK TURBID LIQUID(6,2)\|WELL ANNULAR CEMENT(6,2)\|MAXIMUM SPEED LIMIT(6,1)\|WELL MOUTH(6,1)\|WELLHEAD GAS FLOWMETER(6,1)\|WELLHEAD VENT VALVE(6,1)\|ABANDONED DRILLED WELL(5,4)\|CARBON DIOXIDE STORAGE RESERVOIR(5,4)\|ABANDONED WELL LOGGING INFORMATION(5,2)\|CARBON NEUTRALIZATION(5,2)\|FINE CRACK(5,2)\|FORMATION PERMEABILITY(5,2)\|PACKER DISTANCE(5,2)\|STIRRING BOX(5,2)\|COMPACT WHOLE FIRMNESS(5,1)\|FORMATION TEMPERATURE2THE SOLUBILITY(5,1)\|OVERLYING STRATUM(5,1)\|PROJECT DEMONSTRATION(5,1)\|VOLCANIC ASH CEMENT(5,1)\|WELL DRILLING(4,6)\|LAYER PROTECTION(4,3)\|WELL SEALING(4,2)\|ABANDONED DRILLING(4,1)\|CRACK PORT(4,1)\|FRACTURE LEAKAGE(4,1)\|GEOLOGICAL SEALING(4,1)\|LIME MILK SUSPENSION REACTION(4,1)\|PERFORATION INTERVAL(4,1)\|PERFORATION ZONE(4,1)\|PERMEABILITY CALCULATION(4,1)\|REPAIR DIFFICULTY(4,1)\|WELLHEAD PERIMETER CARBON DIOXIDE(4,1)\|INJECTION TERMINATION SET PRESSURE(3,4)\|CONTINUITY(3,2)\|SET INJECTION TERMINATION PRESSURE(3,2)\|BLOWOUT PREVENTER COMPONENT(3,1)\|CARBON DIOXIDE LEAKAGE PLUGGING(3,1)\|CARBON DIOXIDE RESERVOIR0AND(3,1)\|CONJECTURE(3,1)\|FOSSIL ENERGY(3,1)\|IDENTIFYING LEAKAGE(3,1)\|LEAKAGE REASON(3,1)\|	(CN113494265)\|1. A plugging method for leakage along an abandoned well in a carbon dioxide geological storage process is characterized by comprising the following steps of: the method comprises the following steps:\|step 1: perforating, namely perforating a perforating section formed on the inner wall of the shaft corresponding to the thickness of the stable covering layer, and communicating the annular cement of the drilling well with cracks of the surrounding rock breaking zone;\|step 2: injecting lime milk suspension, namely injecting the lime milk suspension into the perforation, so that the lime milk suspension enters the crack and reacts with leaked carbon dioxide to form calcium carbonate, and further plugging a leakage channel of the carbon dioxide;\|the plugging method further comprises at least one of the following steps:\|prior to step 1, comprising:\|a leakage identification step of identifying whether or not the abandoned well has carbon dioxide leaked along the well; and/or the number of the groups of groups,\|cleaning the inside of the well, namely cleaning a sealing bridge plug in the well before sealing the leaked abandoned well, and ensuring the smoothness and smoothness of the inner wall of the well shaft above the carbon dioxide geological sealing storage layer;\|and/or the number of the groups of groups,\|after step 2, it includes:\|a plugging effect monitoring step, namely monitoring the plugging effect of the well drilling after plugging; and/or, well sealing, namely, sealing the well by an in-well bridge plug for the well drilling after the well is plugged;\|in the step (1) of the process,\|before perforation, a relatively closed space is arranged in the well corresponding to the cover layer part, and the perforation section is arranged in the space; and/or the number of the groups of groups,\|in the step 2 of the process, the process is carried out,\|injecting lime milk suspension through a fracturing truck; and/or when injection begins, the injection pressure P is less than the reservoir pressure P 0 When the concentration of the lime milk suspension is an initial set concentration, and when P is larger than P 0 When the concentration of the lime milk suspension is reduced at a threshold value, the lime milk suspension is continuously injected, and when P is larger than P again 0 And when the threshold value is reached, the concentration of the lime milk suspension is reduced again, then the injection is continued until the concentration of the lime milk suspension is equal to a final set concentration, namely, the injection is continued at the final set concentration until the injection pressure P reaches an injection termination set pressure, and the injection is ended.\|2. The plugging method of claim 1, wherein:\|in the step (1) of the process,\|the aperture of the perforation is controlled to be 5-20 mm; and/or the number of the groups of groups,\|the density of perforation is 10 holes/m-30 holes/m; and/or the number of the groups of groups,\|the depth of perforation is preferably that the drilling annular cement and surrounding rock fracture zone are penetrated; and/or the number of the groups of groups,\|the ratio of the height of the perforation section to the height of the cover layer is 0.1-0.9; and/or the number of the groups of groups,\|the height of the perforating section is between 5 and 30 meters; and/or the number of the groups of groups,\|the distance between the upper edge of the perforation section and the upper edge of the cover layer is more than 5 meters; and/or the number of the groups of groups,\|the spacing between the lower edge of the perforation section and the lower edge of the cap layer is > 5 meters; and/or the number of the groups of groups,\|the perforation sections are uniformly distributed on the whole circumferential surface of the inner wall of the well; and/or the number of the groups of groups,\|the method of determining the position and thickness of the cap layer is at least one of the following:\|(1) Determining the position and thickness of a stable covering layer by analyzing logging and logging data of the abandoned drilling well in the drilling well;\|(2) The location and thickness of the overburden is determined by sonic logging of the abandoned borehole.\|3. The plugging method of claim 1, wherein: the measures for setting the space are as follows: installing an upper packer and a lower packer, wherein the two packers separate carbon dioxide stored in a reservoir layer below the cover layer for storing carbon dioxide and water in an overlying stratum above the cover layer; an injection pipe is arranged on the upper packer, and the pipe orifice at the upper end of the injection pipe is connected with a lime milk suspension injection device arranged on the wellhead, so that lime milk suspension is input into the closed space through the injection pipe and then is injected into the perforation; and/or the number of the groups of groups,\|the threshold value of the difference between the injection pressure P and the reservoir pressure is related to at least one of the following factors:\|(1) The thickness of the cap layer or the thickness of the cap layer and its permeability;\|(2) The permeability of the drilling annulus cement sheath; and/or the number of the groups of groups,\|the threshold is 0.5MPa; and/or the number of the groups of groups,\|the injection pressure is the pressure at the perforation section; and/or the number of the groups of groups,\|the injection termination setting pressure is 1.0MPa; and/or the number of the groups of groups,\|initial set concentration of injected lime milk suspension and injection pressure P and reservoir pressure P of carbon dioxide reservoir 0 Correlation; and/or the number of the groups of groups,\|the initial set concentration of the lime milk suspension is 2-10 mol/L; and/or the number of the groups of groups,\|the injection speed of the lime milk suspension is not higher than 0.5L/s; and/or the number of the groups of groups,\|in the process of injecting lime milk suspension, the injection speed is unchanged; and/or the number of the groups of groups,\|whenever injection pressure P and reservoir pressure P 0 When the difference reaches the threshold value, reducing the multiple of the concentration of the lime milk suspension to be a constant value; and/or the number of the groups of groups,\|the final set concentration is Ca (HO) 2 Solubility at carbon dioxide reservoir temperature.\|4. The plugging method according to claim 3, wherein: in the installation of the packer(s),\|the distance between the packer and the perforating section is more than 2.5 meters; and/or the number of the groups of groups,\|the distance between the packer on the upper part and the upper edge of the cover layer is more than 2.5 meters; and/or the number of the groups of groups,\|the distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters.\|5. The plugging method according to claim 2, wherein: the depth of the perforations is not less than 30 cm.\|6. The plugging method according to claim 3, wherein: the constant value that reduces the multiple of the lime milk suspension concentration is 0.2.\|7. The plugging method of claim 1, wherein: the initial set concentration of the lime milk suspension is 2-10mol/L, when the injection pressure P is greater than the reservoir pressure P 0 And P 0 The pressure difference of (2) exceeds the threshold value by 0.5MPa, the concentration of the lime milk suspension is reduced by 0.2 times of the initial set concentration value, at the moment, the injection pressure P is reduced to ensure that the pressure difference is lower than the threshold value, and the injection pressure is increased as the injection is continued to ensure that the P and the P are formed 0 When the difference of (2) exceeds 0.5MPa again,the concentration of the lime milk suspension is reduced to be 0.2 times of the previous concentration value again, and the process is repeated until the concentration of the lime milk suspension is lower than the solubility of calcium hydroxide at the formation temperature, then the saturated solution of lime milk with the solubility as the concentration enables the injection to be carried out again, the injection pressure is gradually increased, and when P and P are reached 0 When the difference of the two is 1.0MPa, the injection plugging process is finished.\|8. The plugging method of claim 1, wherein:\|in the step of identifying the leak, the leak is identified,\|monitoring the abandoned well for carbon dioxide leakage by at least one of:\|(1) Monitoring the leakage amount of the carbon dioxide at the wellhead;\|(2) Monitoring the wellhead perimeter carbon dioxide concentration to determine a leakage path of carbon dioxide along the abandoned borehole; and/or the number of the groups of groups,\|in the leakage identification step, a blowout prevention protection device is arranged at a wellhead, and an exhaust valve is arranged on the protection device; and/or the number of the groups of groups,\|in the step of cleaning in the well, cleaning a plugging bridge plug in the well shaft through a drilling machine; and/or the number of the groups of groups,\|in the plugging effect monitoring step, at least one of the following measures is taken:\|(1) A monitoring well is drilled beside the abandoned well, the monitoring well is deep above the cover layer, a pH value probe is arranged in the monitoring well, and the leakage condition of carbon dioxide is monitored by monitoring the pH value of formation water;\|(2) Monitoring the amount of leakage of carbon dioxide from the wellhead and/or the periphery of the wellhead of the well; and/or the number of the groups of groups,\|the monitoring frequency is: not less than once every 12 hours; and/or the number of the groups of groups,\|the monitoring period is as follows: after 30 days, no carbon dioxide leakage is found within 30 days, and the good plugging effect is proved; and/or the number of the groups of groups,\|injecting carbon dioxide corrosion resistant cement into the perforation section in the well to form an anti-leakage bridge plug in the well; and/or the number of the groups of groups,\|at least the upper packer is removed prior to cement injection.\|9. The plugging method of claim 8, wherein: the carbon dioxide corrosion resistant cement is: slag cement, pozzolan cement, fly ash cement or composite cement.	(CN113494265)\|TECHNICAL FIELD\|[0001] The invention belongs to the field of geological sealing of greenhouse gases, and relates to a sealing method for leakage along an abandoned well in the geological sealing process of carbon dioxide.\|BACKGROUND ART\|[0002] Carbon dioxide geological sequestration is a carbon dioxide emission reduction technique that injects and permanently sequesters carbon dioxide into geologic bodies such as underground aquifers or abandoned hydrocarbon reservoirs. The method is an emerging carbon dioxide treatment technology with large-scale application potential, and provides a possibility for near zero emission of carbon dioxide used for fossil energy.\|[0003] The government of China has paid great attention to and actively coped with climate change, and has put forward a ' carbon dioxide emission strives to reach a peak before 2030 and strives to achieve a ' ambitious goal of carbon neutralization before 2060 '. To achieve the aim of carbon neutralization, the carbon capturing and sealing technology is the final bottom technology after the maximum emission reduction aim is achieved in industries such as industry, transportation, construction and the like in China. At present, great project demonstration of carbon capture utilization and sealing is developed in each industry of China, and a foundation is laid for subsequent large-scale carbon dioxide injection.\|[0004] Carbon dioxide injected into a reservoir can leak through abandoned borehole, fault or overburden weaknesses due to uncertainty caused by field geological conditions and human development activities, while carbon dioxide leaks along the borehole generally because of chemical or mechanical effects causing carbon dioxide to leak along the borehole annulus cement, wellbore bridge plugs or surrounding rock fracture zones. The current situation is unfavorable for coping with the problem of sudden leakage along abandoned drilling in the carbon dioxide geological sealing process, and the development of the important environmental protection project of underground carbon dioxide sealing is limited to a great extent.\|DISCLOSURE\|Disclosure of Invention\|[0005] The invention aims to solve the problem of leakage of underground carbon dioxide from abandoned wells in the prior art, and provides a method for plugging leakage along abandoned wells in the geological carbon dioxide plugging process.\|[0006] The technical scheme adopted for achieving the purposes of the invention is as follows:\|[0007] a method of plugging leaks along abandoned wells during geological sequestration of carbon dioxide, comprising the steps of:\|[0008] step 1: perforating, namely perforating on the inner wall of the shaft corresponding to the thickness of the stable covering layer, and communicating the annular cement of the drilling well with cracks of the surrounding rock breaking zone;\|[0009] step 2: and injecting lime milk suspension, namely injecting the lime milk suspension into the perforation, so that the lime milk suspension enters the crack and reacts with the leaked carbon dioxide to form calcium carbonate, and further plugging a leakage channel of the carbon dioxide.\|[0010] Preferably, the method comprises the steps of,\|[0011] the plugging method further comprises at least one of the following steps:\|[0012] prior to step 1, it may comprise:\|[0013] and a leakage identification step of identifying whether the abandoned drilling well has carbon dioxide leaked along the drilling well.\|[0014] And cleaning the inside of the well, namely cleaning the sealing bridge plug in the well before sealing the leaked abandoned well, and ensuring the smoothness and smoothness of the inner wall of the well shaft above the carbon dioxide geological sealing storage layer.\|[0015] After step 2, it may include:\|[0016] and a plugging effect monitoring step, namely monitoring the plugging effect of the well drilling after plugging.\|[0017] And (3) well sealing, namely, performing in-well bridge plug well sealing on the well drilling after well sealing.\|[0018] In step 1, the process is preferably performed,\|[0019] a relatively closed space is provided in the wellbore corresponding to the cap layer prior to perforation, in which space the perforated section is disposed.\|[0020] Specifically, installing an upper packer and a lower packer in a well bore, wherein the two packers isolate carbon dioxide sealed in a reservoir in the well bore from water in an overlying stratum; an injection pipe is arranged on the upper packer, and lime cream suspension is input into the closed space through the injection pipe and then is injected into the perforation.\|[0021] In the installation of the packer(s),\|[0022] the distance of the packer from the perforation section is preferably greater than 2.5 meters.\|[0023] The distance of the packer in the upper part from the upper edge of the cover layer is > 2.5 meters.\|[0024] The distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters.\|[0025] Preferably, in said step 1, the step of, in the step of,\|[0026] the aperture of the perforation is controlled to be 5-20 mm.\|[0027] The density of perforations is 10-30 holes/m.\|[0028] The depth of perforation is preferably not less than 30 cm, preferably penetrating the drilling annulus cement and surrounding rock fracture zone.\|[0029] The ratio of the height of the perforation section to the height of the cap layer is 0.1-0.9. The height of the perforation section is preferably between 5 and 30 meters.\|[0030] The spacing between the upper edge of the perforation section and the upper edge of the cap layer is > 5 meters.\|[0031] The spacing between the lower edge of the perforation section and the lower edge of the cap layer is > 5 meters.\|[0032] The perforation sections are uniformly distributed on the whole circumferential surface of the inner wall of the well.\|[0033] In the step 1, the cover layer is referred to as a stable cover layer, which is a protective layer on the carbon dioxide geological sealing storage layer, and can seal the carbon dioxide in the storage layer to prevent the carbon dioxide from escaping upwards, and has the characteristics of high mud content, good continuity, large thickness and the like.\|[0034] The position and thickness of the cap layer are to be determined, and the method of determining the cap layer may be at least one of the following methods:\|[0035] (1) Determining the position and thickness of a stable covering layer by analyzing logging and logging data of the abandoned drilling well in the drilling well;\|[0036] (2) The location and thickness of the overburden is determined by sonic logging of the abandoned borehole.\|[0037] In step 2, preferably, the lime milk suspension is injected by means of a fracturing truck.\|[0038] Initial concentration of injected lime milk suspension and injection pressure P and reservoir pressure P of carbon dioxide reservoir 0 And (5) correlation.\|[0039] When injection begins, the injection pressure P is less than the reservoir pressure P 0 When the concentration of the lime milk suspension is an initial set concentration, and when P is larger than P 0 When the concentration of the lime milk suspension is reduced at a threshold value, the lime milk suspension is continuously injected, and when P is larger than P again 0 And when the threshold value is reached, the concentration of the lime milk suspension is reduced again, then the injection is continued until the concentration of the lime milk suspension is equal to a final set concentration, namely, the injection is continued again with the final set concentration until the injection pressure P reaches an injection termination set pressure, and the injection is ended.\|[0040] Preferably, the method comprises the steps of,\|[0041] the threshold value of the difference between the injection pressure P and the reservoir pressure is related to at least one of the following factors:\|[0042] (1) The thickness of the cap layer or the thickness of the cap layer and its permeability;\|[0043] (2) The permeability of the annulus cement sheath.\|[0044] Preferably, the threshold is 0.5MPa.\|[0045] The injection pressure is the pressure at the perforation section. I.e. the pressure of the enclosed space between the two packers.\|[0046] The injection termination setting pressure is preferably 1.0MPa.\|[0047] Preferably, the initial set concentration of the lime milk suspension is 2-10 mol/liter.\|[0048] Preferably, the injection rate of the lime milk suspension is not higher than 0.5L/s.\|[0049] Preferably, the injection rate is constant during the injection of the lime milk suspension.\|[0050] When the difference between the injection pressure P and the reservoir pressure reaches the threshold value, the multiple of the concentration of the lime milk suspension is reduced to a constant value. Preferably, the constant value is 0.2.\|[0051] The final set concentration is Ca (HO) 2 Solubility at carbon dioxide reservoir temperature.\|[0052] One preferable scheme is as follows: the initial set concentration of the lime milk suspension is 2-10mol/L, when the injection pressure P is greater than the reservoir pressure P 0 And P 0 The pressure difference of (2) exceeds the threshold value by 0.5MPa, the concentration of the lime milk suspension is reduced by 0.2 times of the initial set concentration value, at the moment, the injection pressure P is reduced to ensure that the pressure difference is lower than the threshold value, and the injection pressure is increased as the injection is continued to ensure that the P and the P are formed 0 When the difference value of the concentration of the lime milk suspension exceeds 0.5MPa again, the concentration of the lime milk suspension is reduced to be 0.2 times of the previous concentration value, and the process is repeated circularly until the concentration of the lime milk suspension is lower than the solubility of calcium hydroxide at the formation temperature, then the solubility is used as the concentration of lime milk to be injected, the injection is continued again, the injection pressure is gradually increased, and when P and P are equal to each other 0 When the difference of the two is 1.0MPa, the injection plugging process is finished.\|[0053] Formation temperature may be found from well log and log data of the well, and may also be obtained by methods inferred in the art.\|[0054] In the leak identification step, the leak identification step is preferably,\|[0055] monitoring the abandoned well for carbon dioxide leakage by at least one of:\|[0056] (1) Monitoring the leakage amount of the carbon dioxide at the wellhead;\|[0057] (2) The wellhead perimeter carbon dioxide concentration is monitored to determine the path of leakage of carbon dioxide along the abandoned borehole.\|[0058] Preferably, in the leak identification step, a blowout prevention protection device is provided at the wellhead, and an exhaust valve is provided on the protection device.\|[0059] And closing the exhaust valve when monitoring the carbon dioxide concentration around the wellhead.\|[0060] In the well cleaning step, the plugging bridge plugs in the wellbore are preferably cleaned by a drilling rig.\|[0061] In the plugging effect monitoring step, the plugging effect is preferably,\|[0062] at least one of the following measures is taken:\|[0063] (1) A monitoring well is drilled beside the abandoned well, the monitoring well is deep above the cover layer, a pH value probe is arranged in the monitoring well, and the leakage condition of carbon dioxide is monitored by monitoring the pH value of formation water;\|[0064] (2) The amount of leakage of carbon dioxide from the wellhead and/or the periphery of the wellhead of the well is monitored.\|[0065] Preferably, the method comprises the steps of,\|[0066] the monitoring frequency is: not less than once every 12 hours.\|[0067] The monitoring period is 30 days, and no carbon dioxide leakage is found within 30 days, so that the plugging effect is proved to be good.\|[0068] In the well-sealing step, the well is preferably,\|[0069] and injecting carbon dioxide corrosion resistant cement into the perforation section in the well to form the leakage-proof bridge plug in the well.\|[0070] The upper packer is removed prior to cement injection. The lower packer may be left in the well.\|[0071] The carbon dioxide corrosion resistant cement is preferably: slag cement, pozzolan cement, fly ash cement, composite cement, and the like.\|[0072] The plugging method for plugging leakage along the abandoned well in the geological carbon dioxide plugging process solves the problem of leakage of carbon dioxide from annular cement around abandoned wells and cracks of surrounding rock fracture zones in the carbon dioxide plugging process in the background technology, selects a cover layer with good stratum sealing performance for perforation, communicates a shaft with leakage risk, well annular cement and surrounding rock fracture zones, and can be used for plugging a carbon dioxide leakage channel by injecting lime milk suspension into a perforation section to enable lime milk entering a gap to react with leaked carbon dioxide to form hardened compact calcium carbonate, and simultaneously cementing the surrounding rock fracture zones and the crack-containing well annular cement into a compact whole, thereby greatly reducing the leakage risk along the abandoned well in the geological carbon dioxide plugging process. The invention has the beneficial effects based on the technical scheme that:\|[0073] (1) According to the plugging method, the stable cover layer on the carbon dioxide geological storage layer is preferably used for perforating and plugging the cracks, so that the crack channels leaked along the abandoned well in the carbon dioxide geological storage process can be effectively plugged.\|[0074] (2) According to the plugging method, the lime milk suspension is used for plugging the cracks, hardened and compact calcium carbonate can be generated by the reaction of the lime milk and leaked carbon dioxide in the cracks, a carbon dioxide leakage channel can be effectively plugged, and the formed calcium carbonate can be kept stable under the condition of no external disturbance.\|[0075] (3) According to the plugging method, the concentration of the lime milk suspension injected into the cracks is from high to low, the lime milk suspension with low concentration is more beneficial to entering the fine cracks, and calcium carbonate formed by the reaction of the lime milk suspension and carbon dioxide has a better plugging effect on the cracks.\|[0076] (4) According to the plugging method, lime milk suspension is injected into cracks to react with carbon dioxide to form compact calcium carbonate, and the process can bond a surrounding rock breaking zone and crack-containing drilling annular cement into a compact whole, so that the risk of leakage along an abandoned well in the geological carbon dioxide plugging process is greatly reduced.\|[0077] (5) According to the plugging method, the injected lime milk suspension reacts with the carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, so that the risk of geological environment pollution is extremely low, and the plugging process is safe and environment-friendly.\|[0078] The invention is illustrated in detail below by means of the figures and examples.\|DRAWINGS DESCRIPTION\|[0079] FIG. 1 is a schematic illustration of a plugging process for carbon dioxide leakage along a abandoned well in the present invention.\|[0080] FIG. 2 is a flow chart of the plugging of carbon dioxide leaks along a abandoned well in the present invention.\|INVENTION MODE\|Detailed Description\|[0081] The present invention is described in detail below with reference to fig. 1 and the embodiment. Fig. 1 shows a facility, an arranged plugging structure and equipment for plugging abandoned wells by the plugging method provided by the invention. The plugging method is illustrated by fig. 2.\|[0082] The method comprises the following specific steps of:\|[0083] step 1: identifying leakage;\|[0084] step 2: cleaning in a well;\|[0085] step 3: perforating;\|[0086] step 4: plugging;\|[0087] step 5: monitoring plugging effect;\|[0088] step 6: and (5) sealing the well.\|[0089] The following is a detailed description.\|[0090] Firstly, a leakage identification step is carried out on abandoned wells to find out the leakage position and the leakage amount of carbon dioxide along the abandoned wells, a simple bracket can be arranged at a wellhead, and a gas flowmeter 16 is supported at the wellhead to determine whether the wellhead emits carbon dioxide or not. If a carbon dioxide leak is detected, i.e. the plugging method of the invention is ready to be carried out, the blowout preventer 1 is first installed at the wellhead, and the gas flow meter 16 is a component of the blowout preventer and is arranged on the protector, as shown in fig. 1.\|[0091] The blowout prevention protection device is installed in order to prevent the risk of leakage of a large amount of gas existing after perforation.\|[0092] Another measure of leak identification is: closing an exhaust valve on the blowout preventer, and monitoring the concentration of carbon dioxide at the wellhead perimeter to determine the path of leakage of carbon dioxide along the abandoned wellbore. Judging whether the carbon dioxide leaks through the cracks of the annular cement and the surrounding rock fracture zone of the well drilling or leaks from other parts of the weak cap layer, and if the carbon dioxide leaks from other positions, taking other measures to perform plugging is not the content of the invention and is not repeated herein.\|[0093] And then, carrying out an in-well cleaning step on the well shaft 2, cleaning a cement bridge plug in the well shaft 2 by adopting a drilling machine, and selecting and determining the position and the thickness of the stable cover layer 3 with good stratum sealing performance.\|[0094] The selection of a stable cap layer can be performed by analyzing well logging and logging information, and the position and thickness of the cap layer can be determined by means of sonic detection.\|[0095] The stable cover layer is a protective layer which is arranged on the carbon dioxide geological seal storage layer 9 and can seal the carbon dioxide in the storage layer 9 from upward dissipation, has the characteristics of high clay content, good continuity, large thickness and the like, and the porosity of the cover layer 3 is generally less than 5 percent, and the permeability is less than 1mD.\|[0096] Then, perforating 4 is carried out on the inner wall of the corresponding cover layer 3 of the shaft 2, and the perforating 4 is communicated with the cracks 7 of the drilling annular cement 5 and the surrounding rock breaking belt 6;\|[0097] when drilling is excavated, after the shaft 2 passes through the cover layer 3, the cover layer around the shaft 2 is damaged, annular cement 5 and surrounding rock breaking zones 6 are formed around the shaft 2, and cracks 7 are large, so that carbon dioxide in a reservoir layer leaks out through the cracks 7. The plugging method of the invention is to plug the leakage.\|[0098] A relatively closed space is required in the wellbore 2 at the perforation interval at the corresponding cap prior to perforation to avoid the risk of significant amounts of carbon dioxide and water entering the wellbore 2 during perforation. The measures for setting the closed space are as follows: installing an upper packer 8 and a lower packer 8 on the inner wall of the well shaft corresponding to the cover layer 3 in the well shaft 2, wherein the two packers 8 isolate carbon dioxide sealed in a reservoir 9 below the cover layer 3 from water in an overburden stratum 10 above the cover layer; an injection pipe, also called a central pipe 18, is arranged on the upper packer 8, the upper pipe orifice of the central pipe 18 is connected with a lime milk suspension injection device fracturing truck 12 arranged on the wellhead, the fracturing truck 12 is connected with a stirring box, and lime milk suspension with required concentration is provided, so that the lime milk suspension is input into the closed space through the injection pipe at a certain speed, and then is injected into the perforation.\|[0099] Preferably, the distance of the packer from the perforation section during the step of setting the packer is greater than 2.5m. The distance of the packer in the upper part from the upper edge of the cover layer is > 2.5 meters. The distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters. The aperture of the perforations 4 is controlled to be 5-20mm, in this embodiment, for example, 7mm. The density of perforations is 10 holes/meter-30 holes/meter, in this embodiment, 20 holes/meter in the perforation section. The ratio of the height of the perforating section to the height of the cover layer is 0.1-0.9, the ratio value is selected in relation to the thickness of the cover layer, the thickness of the cover layer is generally tens of meters to hundreds of meters, when the thickness of the cover layer is thinner, the ratio value is slightly larger, and when the thickness of the cover layer is thicker, the ratio value is slightly smaller, so that the height of the perforating section is ensured to be more suitable for 5-30 meters. Preferably, the spacing between the upper and lower edges of the perforation section and the upper and lower edges of the cap layer is greater than 5 meters. In this embodiment, both pitches are, for example, 8 meters.\|[0100] According to the invention, lime milk is injected into the perforation of the cover layer, and on annular cement and surrounding rock fracture zones where cracks appear due to the damage of drilling on the cover layer, the lime milk and carbon dioxide meet and react in the cracks to generate calcium carbonate to fill and seal the cracks, so that the cover layer is repaired. Therefore, the aperture and density of the perforation can influence the state that the lime milk suspension enters the cracks, if the aperture of the perforation is too small, the flow of the lime milk can be blocked, so that the contact between the lime milk and the carbon dioxide is poor, but if the aperture is too large, the cover layer can be damaged greatly, the repairing difficulty is increased, and the distribution of the lime milk in the drilling annulus cement 5 and the surrounding rock breaking zone 6 can be influenced by the density of the perforation. The proper aperture and density of the perforation are selected, and the position and the height of the perforation section in the cover layer can influence the stability and the firmness of cementing the surrounding rock breaking zone and the annular cement of the fractured well into a compact whole and the high efficiency of plugging construction.\|[0101] It is also a good measure that the perforation segments are evenly distributed over the entire circumference of the inner wall of the well. Because the crack position is not well controlled, the position where the crack possibly appears can be fully covered by the uniform perforation, and a better plugging effect can be obtained.\|[0102] The next step is to perform the plugging by injecting a lime milk suspension into the enclosed space, i.e. into the perforations 4. Preparing lime milk suspension (Ca (HO) with initial set concentration not less than 2mol/L (2-10 mol/L) by using a stirring box 11 arranged on a wellhead 2 Colloidal solution), for example, an initial set concentration of 5mol/L, is slowly injected into the perforation section by means of the fracturing unit 12 through the central conduit 18 at a rate of less than 0.5L/s, for example, 0.3L/s, when the injection pressure P is higher than the reservoir pressure P 0 A threshold value, for example, 0.5MPa, which is a value of 0.2 times the initial injection concentration, i.e., the concentration is reduced to 1mol/L, and then the injection is continued slowly at a rate of 0.3L/s, and when the injection pressure P is raised again by a threshold value of 0.5MPa, the concentration of the lime milk suspension is reduced again to 0.2 times the previous concentration, i.e., the concentration is reduced to 0.2mol/L, and the injection is continued, and the cycle is continued until the lime milk concentration is equal to or less than the formation temperature, i.e., the temperature of the carbon dioxide reservoir 9, ca (HO 2 For example, the temperature of reservoir 9 is 60 ℃, ca (HO) at this time 2 The solubility of (C) was 0.02mol/L. Thus, when the injection pressure is increased by two more thresholds, the concentration of milk of lime is reduced to Ca (HO) at the formation temperature 2 Is a solvent for the polymer. At this time, the injection was continued at a concentration of 0.02mol/L, the concentration of lime milk was not lowered any more, and the above-mentioned solubility was the final set concentration. Continuing the injection at this final set concentration, the injection pressure gradually increases and, when increasing to an injection termination set pressure, the injection ends. This injection termination set pressure was 1.0MPa.\|[0103] As another example, where the initial set concentration of milk of lime is 10mol/L, the threshold value is also 0.5MPa when the injection pressure P reaches a value higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 2mol/L, the injection is continued, and when the injection pressure P is higher than the reservoir pressure P again 0 At 0.5MPa, the concentration is reduced to 0.4 mol/L again, the injection is continued, and the third injection pressure is higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 0.08 mol/L, and the fourth injection pressure is higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 0.016 mol/L, which is lower than the solution degree of 0.02mol/L, and at this time, the solution is injected at the final set concentration, namely the solubility, until the injection pressure is 1.0MPa.\|[0104] The pressure difference of the threshold value and the thickness of the cement sheath can calculate the stratum permeability, and when the parameters are set, the calculated stratum permeability of the cement sheath is close to the stratum permeability of the cover layer, and the closed crack under the lime milk concentration condition can be considered to be not leaked. The fact that a threshold value is reached indicates that the lime milk with the existing concentration is not easy to continue to be injected, so that the concentration needs to be reduced, the concentration is reduced by a constant multiple, the operation is facilitated, and more importantly, the completion of plugging of fine cracks can be achieved gradually.\|[0105] In the injection process, the concentration of lime milk is adjusted, and initially, the concentration is larger, larger cracks are filled as soon as possible, then the concentration is reduced, lime milk with lower concentration easily enters smaller cracks, and fine cracks can be plugged. At the initial set concentration, the plugging can be completed within 10 times of concentration reduction according to the rate reduction of 0.2 times, and the setting is ideal. If the initial set concentration is too low, an integral structure with good plugging performance is not easy to form. However, if the initial set concentration is too high, the lime milk is too thick, and besides the problems of the above and the increase of the concentration reduction times, ports of some cracks are sealed by the thick lime milk, so that the whole annular cement and the size cracks in the surrounding rock breaking zone are not filled, and the sealing effect is also affected.\|[0106] The lowest final set concentration of milk of lime is not lower than the solubility at the temperature of the reservoir 9, which serves to let the milk of lime suspension sufficiently enter the fissures 7 at a set final set pressure (e.g. 1.0 MPa). But the final set concentration must not be below the solution level, otherwise, the subsequent injection of unsaturated lime water will have a damaging effect on the calcium carbonate formed by the reaction of the previously injected lime milk with carbon dioxide.\|[0107] The injection rate described above also affects the occlusion effect. The invention provides a maximum rate limit of 0.5 liter/second at which lime milk entering the crack can react with leaked carbon dioxide in good time to form calcium carbonate to seal the crack. If the speed limit is too high, the blocking effect is not good, but if the speed limit is too low, the blocking is not easy to proceed and the blocking efficiency is too low.\|[0108] The plugging effect monitoring step follows.\|[0109] Monitoring can also be performed by using a gas flow meter provided at the wellhead to measure the gas flow at the wellhead. A wellhead vent valve, which is a valve to a gas flow meter, may also be closed, and the wellhead perimeter carbon dioxide concentration monitored to determine the leak path of carbon dioxide along the abandoned borehole.\|[0110] Alternatively, a monitoring well 13 may be drilled on the side of the well, the well depth of which does not exceed the cap layer 3.\|[0111] Ph value probes (14), an earth surface carbon dioxide concentration meter (15) and a wellhead gas flowmeter (16) are placed in a monitoring well (13) to be matched for use, the Ph value of overlying stratum water, the wellhead periphery carbon dioxide concentration and wellhead carbon dioxide leakage are continuously monitored, and data are analyzed through an earth surface monitoring station (17).\|[0112] The frequency of monitoring may be generally such that data is taken every 12 hours.\|[0113] If no carbon dioxide leakage is found in the 30-day monitoring, the plugging is considered to be successful, and then the following process steps are carried out: and (5) sealing the well.\|[0114] The bridge plug well sealing in the well can be implemented, and the sealing of the leakage of the carbon dioxide along the abandoned well is completed.\|[0115] Firstly, taking out the packer at the upper part of the perforation section, injecting carbon dioxide corrosion resistant cement and the like into the perforation section in the well to form a cement bridge plug for preventing leakage in the well, and integrally completing the plugging of the leakage of carbon dioxide along the abandoned well. The carbon dioxide corrosion resistant cement can be slag cement, volcanic ash cement, fly ash cement or composite cement, etc., and the concrete method of well sealing belongs to the prior art and is not repeated here.\|[0116] If the sealing is not up to standard through monitoring, the leakage reason needs to be specifically analyzed, if the leakage is still caused by the crack around the drilling well, the perforation 4 can be set at a new position again, lime milk can be refilled, at this time, the concentration of the lime milk can be adjusted, for example, the set concentration is increased, and the lime milk can be refilled. And then monitoring the blocking effect until the blocking reaches the standard.\|[0117] According to the invention, the cover layer is preferably perforated, a shaft with leakage risk, drilling annulus cement and a surrounding rock breaking belt are communicated, a packer is arranged in the shaft, a relatively closed space is formed in a perforation section, lime milk suspension is slowly injected into the perforation section through a fracturing truck, the injection pressure is controlled in the process, the concentration of lime milk is gradually reduced, lime milk in a crack reacts with leaked carbon dioxide to form hardened and compact calcium carbonate, and a carbon dioxide leakage channel is further plugged. The invention can effectively block the crack channel leaked along the abandoned well in the geological carbon dioxide sealing process, and can bond the surrounding rock breaking zone and the crack-containing drilling annular cement into a compact whole, thereby greatly reducing the risk of leakage along the abandoned well in the geological carbon dioxide sealing process. The injected lime milk suspension reacts with the carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, so that the risk of geological environment pollution is extremely low, and the plugging process is safe and environment-friendly.	(CN113494265)\|TECHNICAL FIELD\|[0001] The invention belongs to the field of geological sealing of greenhouse gases, and relates to a sealing method for leakage along an abandoned well in the geological sealing process of carbon dioxide.\|BACKGROUND ART\|[0002] Carbon dioxide geological sequestration is a carbon dioxide emission reduction technique that injects and permanently sequesters carbon dioxide into geologic bodies such as underground aquifers or abandoned hydrocarbon reservoirs. The method is an emerging carbon dioxide treatment technology with large-scale application potential, and provides a possibility for near zero emission of carbon dioxide used for fossil energy.\|[0003] The government of China has paid great attention to and actively coped with climate change, and has put forward a ' carbon dioxide emission strives to reach a peak before 2030 and strives to achieve a ' ambitious goal of carbon neutralization before 2060 '. To achieve the aim of carbon neutralization, the carbon capturing and sealing technology is the final bottom technology after the maximum emission reduction aim is achieved in industries such as industry, transportation, construction and the like in China. At present, great project demonstration of carbon capture utilization and sealing is developed in each industry of China, and a foundation is laid for subsequent large-scale carbon dioxide injection.\|[0004] Carbon dioxide injected into a reservoir can leak through abandoned borehole, fault or overburden weaknesses due to uncertainty caused by field geological conditions and human development activities, while carbon dioxide leaks along the borehole generally because of chemical or mechanical effects causing carbon dioxide to leak along the borehole annulus cement, wellbore bridge plugs or surrounding rock fracture zones. The current situation is unfavorable for coping with the problem of sudden leakage along abandoned drilling in the carbon dioxide geological sealing process, and the development of the important environmental protection project of underground carbon dioxide sealing is limited to a great extent.\|DISCLOSURE\|Disclosure of Invention\|[0005] The invention aims to solve the problem of leakage of underground carbon dioxide from abandoned wells in the prior art, and provides a method for plugging leakage along abandoned wells in the geological carbon dioxide plugging process.\|[0006] The technical scheme adopted for achieving the purposes of the invention is as follows:\|[0007] a method of plugging leaks along abandoned wells during geological sequestration of carbon dioxide, comprising the steps of:\|[0008] step 1: perforating, namely perforating on the inner wall of the shaft corresponding to the thickness of the stable covering layer, and communicating the annular cement of the drilling well with cracks of the surrounding rock breaking zone;\|[0009] step 2: and injecting lime milk suspension, namely injecting the lime milk suspension into the perforation, so that the lime milk suspension enters the crack and reacts with the leaked carbon dioxide to form calcium carbonate, and further plugging a leakage channel of the carbon dioxide.\|[0010] Preferably, the method comprises the steps of,\|[0011] the plugging method further comprises at least one of the following steps:\|[0012] prior to step 1, it may comprise:\|[0013] and a leakage identification step of identifying whether the abandoned drilling well has carbon dioxide leaked along the drilling well.\|[0014] And cleaning the inside of the well, namely cleaning the sealing bridge plug in the well before sealing the leaked abandoned well, and ensuring the smoothness and smoothness of the inner wall of the well shaft above the carbon dioxide geological sealing storage layer.\|[0015] After step 2, it may include:\|[0016] and a plugging effect monitoring step, namely monitoring the plugging effect of the well drilling after plugging.\|[0017] And (3) well sealing, namely, performing in-well bridge plug well sealing on the well drilling after well sealing.\|[0018] In step 1, the process is preferably performed,\|[0019] a relatively closed space is provided in the wellbore corresponding to the cap layer prior to perforation, in which space the perforated section is disposed.\|[0020] Specifically, installing an upper packer and a lower packer in a well bore, wherein the two packers isolate carbon dioxide sealed in a reservoir in the well bore from water in an overlying stratum; an injection pipe is arranged on the upper packer, and lime cream suspension is input into the closed space through the injection pipe and then is injected into the perforation.\|[0021] In the installation of the packer(s),\|[0022] the distance of the packer from the perforation section is preferably greater than 2.5 meters.\|[0023] The distance of the packer in the upper part from the upper edge of the cover layer is > 2.5 meters.\|[0024] The distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters.\|[0025] Preferably, in said step 1, the step of, in the step of,\|[0026] the aperture of the perforation is controlled to be 5-20 mm.\|[0027] The density of perforations is 10-30 holes/m.\|[0028] The depth of perforation is preferably not less than 30 cm, preferably penetrating the drilling annulus cement and surrounding rock fracture zone.\|[0029] The ratio of the height of the perforation section to the height of the cap layer is 0.1-0.9. The height of the perforation section is preferably between 5 and 30 meters.\|[0030] The spacing between the upper edge of the perforation section and the upper edge of the cap layer is > 5 meters.\|[0031] The spacing between the lower edge of the perforation section and the lower edge of the cap layer is > 5 meters.\|[0032] The perforation sections are uniformly distributed on the whole circumferential surface of the inner wall of the well.\|[0033] In the step 1, the cover layer is referred to as a stable cover layer, which is a protective layer on the carbon dioxide geological sealing storage layer, and can seal the carbon dioxide in the storage layer to prevent the carbon dioxide from escaping upwards, and has the characteristics of high mud content, good continuity, large thickness and the like.\|[0034] The position and thickness of the cap layer are to be determined, and the method of determining the cap layer may be at least one of the following methods:\|[0035] (1) Determining the position and thickness of a stable covering layer by analyzing logging and logging data of the abandoned drilling well in the drilling well;\|[0036] (2) The location and thickness of the overburden is determined by sonic logging of the abandoned borehole.\|[0037] In step 2, preferably, the lime milk suspension is injected by means of a fracturing truck.\|[0038] Initial concentration of injected lime milk suspension and injection pressure P and reservoir pressure P of carbon dioxide reservoir 0 And (5) correlation.\|[0039] When injection begins, the injection pressure P is less than the reservoir pressure P 0 When the concentration of the lime milk suspension is an initial set concentration, and when P is larger than P 0 When the concentration of the lime milk suspension is reduced at a threshold value, the lime milk suspension is continuously injected, and when P is larger than P again 0 And when the threshold value is reached, the concentration of the lime milk suspension is reduced again, then the injection is continued until the concentration of the lime milk suspension is equal to a final set concentration, namely, the injection is continued again with the final set concentration until the injection pressure P reaches an injection termination set pressure, and the injection is ended.\|[0040] Preferably, the method comprises the steps of,\|[0041] the threshold value of the difference between the injection pressure P and the reservoir pressure is related to at least one of the following factors:\|[0042] (1) The thickness of the cap layer or the thickness of the cap layer and its permeability;\|[0043] (2) The permeability of the annulus cement sheath.\|[0044] Preferably, the threshold is 0.5MPa.\|[0045] The injection pressure is the pressure at the perforation section. I.e. the pressure of the enclosed space between the two packers.\|[0046] The injection termination setting pressure is preferably 1.0MPa.\|[0047] Preferably, the initial set concentration of the lime milk suspension is 2-10 mol/liter.\|[0048] Preferably, the injection rate of the lime milk suspension is not higher than 0.5L/s.\|[0049] Preferably, the injection rate is constant during the injection of the lime milk suspension.\|[0050] When the difference between the injection pressure P and the reservoir pressure reaches the threshold value, the multiple of the concentration of the lime milk suspension is reduced to a constant value. Preferably, the constant value is 0.2.\|[0051] The final set concentration is Ca (HO) 2 Solubility at carbon dioxide reservoir temperature.\|[0052] One preferable scheme is as follows: the initial set concentration of the lime milk suspension is 2-10mol/L, when the injection pressure P is greater than the reservoir pressure P 0 And P 0 The pressure difference of (2) exceeds the threshold value by 0.5MPa, the concentration of the lime milk suspension is reduced by 0.2 times of the initial set concentration value, at the moment, the injection pressure P is reduced to ensure that the pressure difference is lower than the threshold value, and the injection pressure is increased as the injection is continued to ensure that the P and the P are formed 0 When the difference value of the concentration of the lime milk suspension exceeds 0.5MPa again, the concentration of the lime milk suspension is reduced to be 0.2 times of the previous concentration value, and the process is repeated circularly until the concentration of the lime milk suspension is lower than the solubility of calcium hydroxide at the formation temperature, then the solubility is used as the concentration of lime milk to be injected, the injection is continued again, the injection pressure is gradually increased, and when P and P are equal to each other 0 When the difference of the two is 1.0MPa, the injection plugging process is finished.\|[0053] Formation temperature may be found from well log and log data of the well, and may also be obtained by methods inferred in the art.\|[0054] In the leak identification step, the leak identification step is preferably,\|[0055] monitoring the abandoned well for carbon dioxide leakage by at least one of:\|[0056] (1) Monitoring the leakage amount of the carbon dioxide at the wellhead;\|[0057] (2) The wellhead perimeter carbon dioxide concentration is monitored to determine the path of leakage of carbon dioxide along the abandoned borehole.\|[0058] Preferably, in the leak identification step, a blowout prevention protection device is provided at the wellhead, and an exhaust valve is provided on the protection device.\|[0059] And closing the exhaust valve when monitoring the carbon dioxide concentration around the wellhead.\|[0060] In the well cleaning step, the plugging bridge plugs in the wellbore are preferably cleaned by a drilling rig.\|[0061] In the plugging effect monitoring step, the plugging effect is preferably,\|[0062] at least one of the following measures is taken:\|[0063] (1) A monitoring well is drilled beside the abandoned well, the monitoring well is deep above the cover layer, a pH value probe is arranged in the monitoring well, and the leakage condition of carbon dioxide is monitored by monitoring the pH value of formation water;\|[0064] (2) The amount of leakage of carbon dioxide from the wellhead and/or the periphery of the wellhead of the well is monitored.\|[0065] Preferably, the method comprises the steps of,\|[0066] the monitoring frequency is: not less than once every 12 hours.\|[0067] The monitoring period is 30 days, and no carbon dioxide leakage is found within 30 days, so that the plugging effect is proved to be good.\|[0068] In the well-sealing step, the well is preferably,\|[0069] and injecting carbon dioxide corrosion resistant cement into the perforation section in the well to form the leakage-proof bridge plug in the well.\|[0070] The upper packer is removed prior to cement injection. The lower packer may be left in the well.\|[0071] The carbon dioxide corrosion resistant cement is preferably: slag cement, pozzolan cement, fly ash cement, composite cement, and the like.\|[0072] The plugging method for plugging leakage along the abandoned well in the geological carbon dioxide plugging process solves the problem of leakage of carbon dioxide from annular cement around abandoned wells and cracks of surrounding rock fracture zones in the carbon dioxide plugging process in the background technology, selects a cover layer with good stratum sealing performance for perforation, communicates a shaft with leakage risk, well annular cement and surrounding rock fracture zones, and can be used for plugging a carbon dioxide leakage channel by injecting lime milk suspension into a perforation section to enable lime milk entering a gap to react with leaked carbon dioxide to form hardened compact calcium carbonate, and simultaneously cementing the surrounding rock fracture zones and the crack-containing well annular cement into a compact whole, thereby greatly reducing the leakage risk along the abandoned well in the geological carbon dioxide plugging process. The invention has the beneficial effects based on the technical scheme that:\|[0073] (1) According to the plugging method, the stable cover layer on the carbon dioxide geological storage layer is preferably used for perforating and plugging the cracks, so that the crack channels leaked along the abandoned well in the carbon dioxide geological storage process can be effectively plugged.\|[0074] (2) According to the plugging method, the lime milk suspension is used for plugging the cracks, hardened and compact calcium carbonate can be generated by the reaction of the lime milk and leaked carbon dioxide in the cracks, a carbon dioxide leakage channel can be effectively plugged, and the formed calcium carbonate can be kept stable under the condition of no external disturbance.\|[0075] (3) According to the plugging method, the concentration of the lime milk suspension injected into the cracks is from high to low, the lime milk suspension with low concentration is more beneficial to entering the fine cracks, and calcium carbonate formed by the reaction of the lime milk suspension and carbon dioxide has a better plugging effect on the cracks.\|[0076] (4) According to the plugging method, lime milk suspension is injected into cracks to react with carbon dioxide to form compact calcium carbonate, and the process can bond a surrounding rock breaking zone and crack-containing drilling annular cement into a compact whole, so that the risk of leakage along an abandoned well in the geological carbon dioxide plugging process is greatly reduced.\|[0077] (5) According to the plugging method, the injected lime milk suspension reacts with the carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, so that the risk of geological environment pollution is extremely low, and the plugging process is safe and environment-friendly.\|[0078] The invention is illustrated in detail below by means of the figures and examples.\|DRAWINGS DESCRIPTION\|[0079] FIG. 1 is a schematic illustration of a plugging process for carbon dioxide leakage along a abandoned well in the present invention.\|[0080] FIG. 2 is a flow chart of the plugging of carbon dioxide leaks along a abandoned well in the present invention.\|INVENTION MODE\|Detailed Description\|[0081] The present invention is described in detail below with reference to fig. 1 and the embodiment. Fig. 1 shows a facility, an arranged plugging structure and equipment for plugging abandoned wells by the plugging method provided by the invention. The plugging method is illustrated by fig. 2.\|[0082] The method comprises the following specific steps of:\|[0083] step 1: identifying leakage;\|[0084] step 2: cleaning in a well;\|[0085] step 3: perforating;\|[0086] step 4: plugging;\|[0087] step 5: monitoring plugging effect;\|[0088] step 6: and (5) sealing the well.\|[0089] The following is a detailed description.\|[0090] Firstly, a leakage identification step is carried out on abandoned wells to find out the leakage position and the leakage amount of carbon dioxide along the abandoned wells, a simple bracket can be arranged at a wellhead, and a gas flowmeter 16 is supported at the wellhead to determine whether the wellhead emits carbon dioxide or not. If a carbon dioxide leak is detected, i.e. the plugging method of the invention is ready to be carried out, the blowout preventer 1 is first installed at the wellhead, and the gas flow meter 16 is a component of the blowout preventer and is arranged on the protector, as shown in fig. 1.\|[0091] The blowout prevention protection device is installed in order to prevent the risk of leakage of a large amount of gas existing after perforation.\|[0092] Another measure of leak identification is: closing an exhaust valve on the blowout preventer, and monitoring the concentration of carbon dioxide at the wellhead perimeter to determine the path of leakage of carbon dioxide along the abandoned wellbore. Judging whether the carbon dioxide leaks through the cracks of the annular cement and the surrounding rock fracture zone of the well drilling or leaks from other parts of the weak cap layer, and if the carbon dioxide leaks from other positions, taking other measures to perform plugging is not the content of the invention and is not repeated herein.\|[0093] And then, carrying out an in-well cleaning step on the well shaft 2, cleaning a cement bridge plug in the well shaft 2 by adopting a drilling machine, and selecting and determining the position and the thickness of the stable cover layer 3 with good stratum sealing performance.\|[0094] The selection of a stable cap layer can be performed by analyzing well logging and logging information, and the position and thickness of the cap layer can be determined by means of sonic detection.\|[0095] The stable cover layer is a protective layer which is arranged on the carbon dioxide geological seal storage layer 9 and can seal the carbon dioxide in the storage layer 9 from upward dissipation, has the characteristics of high clay content, good continuity, large thickness and the like, and the porosity of the cover layer 3 is generally less than 5 percent, and the permeability is less than 1mD.\|[0096] Then, perforating 4 is carried out on the inner wall of the corresponding cover layer 3 of the shaft 2, and the perforating 4 is communicated with the cracks 7 of the drilling annular cement 5 and the surrounding rock breaking belt 6;\|[0097] when drilling is excavated, after the shaft 2 passes through the cover layer 3, the cover layer around the shaft 2 is damaged, annular cement 5 and surrounding rock breaking zones 6 are formed around the shaft 2, and cracks 7 are large, so that carbon dioxide in a reservoir layer leaks out through the cracks 7. The plugging method of the invention is to plug the leakage.\|[0098] A relatively closed space is required in the wellbore 2 at the perforation interval at the corresponding cap prior to perforation to avoid the risk of significant amounts of carbon dioxide and water entering the wellbore 2 during perforation. The measures for setting the closed space are as follows: installing an upper packer 8 and a lower packer 8 on the inner wall of the well shaft corresponding to the cover layer 3 in the well shaft 2, wherein the two packers 8 isolate carbon dioxide sealed in a reservoir 9 below the cover layer 3 from water in an overburden stratum 10 above the cover layer; an injection pipe, also called a central pipe 18, is arranged on the upper packer 8, the upper pipe orifice of the central pipe 18 is connected with a lime milk suspension injection device fracturing truck 12 arranged on the wellhead, the fracturing truck 12 is connected with a stirring box, and lime milk suspension with required concentration is provided, so that the lime milk suspension is input into the closed space through the injection pipe at a certain speed, and then is injected into the perforation.\|[0099] Preferably, the distance of the packer from the perforation section during the step of setting the packer is greater than 2.5m. The distance of the packer in the upper part from the upper edge of the cover layer is > 2.5 meters. The distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters. The aperture of the perforations 4 is controlled to be 5-20mm, in this embodiment, for example, 7mm. The density of perforations is 10 holes/meter-30 holes/meter, in this embodiment, 20 holes/meter in the perforation section. The ratio of the height of the perforating section to the height of the cover layer is 0.1-0.9, the ratio value is selected in relation to the thickness of the cover layer, the thickness of the cover layer is generally tens of meters to hundreds of meters, when the thickness of the cover layer is thinner, the ratio value is slightly larger, and when the thickness of the cover layer is thicker, the ratio value is slightly smaller, so that the height of the perforating section is ensured to be more suitable for 5-30 meters. Preferably, the spacing between the upper and lower edges of the perforation section and the upper and lower edges of the cap layer is greater than 5 meters. In this embodiment, both pitches are, for example, 8 meters.\|[0100] According to the invention, lime milk is injected into the perforation of the cover layer, and on annular cement and surrounding rock fracture zones where cracks appear due to the damage of drilling on the cover layer, the lime milk and carbon dioxide meet and react in the cracks to generate calcium carbonate to fill and seal the cracks, so that the cover layer is repaired. Therefore, the aperture and density of the perforation can influence the state that the lime milk suspension enters the cracks, if the aperture of the perforation is too small, the flow of the lime milk can be blocked, so that the contact between the lime milk and the carbon dioxide is poor, but if the aperture is too large, the cover layer can be damaged greatly, the repairing difficulty is increased, and the distribution of the lime milk in the drilling annulus cement 5 and the surrounding rock breaking zone 6 can be influenced by the density of the perforation. The proper aperture and density of the perforation are selected, and the position and the height of the perforation section in the cover layer can influence the stability and the firmness of cementing the surrounding rock breaking zone and the annular cement of the fractured well into a compact whole and the high efficiency of plugging construction.\|[0101] It is also a good measure that the perforation segments are evenly distributed over the entire circumference of the inner wall of the well. Because the crack position is not well controlled, the position where the crack possibly appears can be fully covered by the uniform perforation, and a better plugging effect can be obtained.\|[0102] The next step is to perform the plugging by injecting a lime milk suspension into the enclosed space, i.e. into the perforations 4. Preparing lime milk suspension (Ca (HO) with initial set concentration not less than 2mol/L (2-10 mol/L) by using a stirring box 11 arranged on a wellhead 2 Colloidal solution), for example, an initial set concentration of 5mol/L, is slowly injected into the perforation section by means of the fracturing unit 12 through the central conduit 18 at a rate of less than 0.5L/s, for example, 0.3L/s, when the injection pressure P is higher than the reservoir pressure P 0 A threshold value, for example, 0.5MPa, which is a value of 0.2 times the initial injection concentration, i.e., the concentration is reduced to 1mol/L, and then the injection is continued slowly at a rate of 0.3L/s, and when the injection pressure P is raised again by a threshold value of 0.5MPa, the concentration of the lime milk suspension is reduced again to 0.2 times the previous concentration, i.e., the concentration is reduced to 0.2mol/L, and the injection is continued, and the cycle is continued until the lime milk concentration is equal to or less than the formation temperature, i.e., the temperature of the carbon dioxide reservoir 9, ca (HO 2 For example, the temperature of reservoir 9 is 60 ℃, ca (HO) at this time 2 The solubility of (C) was 0.02mol/L. Thus, when the injection pressure is increased by two more thresholds, the concentration of milk of lime is reduced to Ca (HO) at the formation temperature 2 Is a solvent for the polymer. At this time, the injection was continued at a concentration of 0.02mol/L, the concentration of lime milk was not lowered any more, and the above-mentioned solubility was the final set concentration. Continuing the injection at this final set concentration, the injection pressure gradually increases and, when increasing to an injection termination set pressure, the injection ends. This injection termination set pressure was 1.0MPa.\|[0103] As another example, where the initial set concentration of milk of lime is 10mol/L, the threshold value is also 0.5MPa when the injection pressure P reaches a value higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 2mol/L, the injection is continued, and when the injection pressure P is higher than the reservoir pressure P again 0 At 0.5MPa, the concentration is reduced to 0.4 mol/L again, the injection is continued, and the third injection pressure is higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 0.08 mol/L, and the fourth injection pressure is higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 0.016 mol/L, which is lower than the solution degree of 0.02mol/L, and at this time, the solution is injected at the final set concentration, namely the solubility, until the injection pressure is 1.0MPa.\|[0104] The pressure difference of the threshold value and the thickness of the cement sheath can calculate the stratum permeability, and when the parameters are set, the calculated stratum permeability of the cement sheath is close to the stratum permeability of the cover layer, and the closed crack under the lime milk concentration condition can be considered to be not leaked. The fact that a threshold value is reached indicates that the lime milk with the existing concentration is not easy to continue to be injected, so that the concentration needs to be reduced, the concentration is reduced by a constant multiple, the operation is facilitated, and more importantly, the completion of plugging of fine cracks can be achieved gradually.\|[0105] In the injection process, the concentration of lime milk is adjusted, and initially, the concentration is larger, larger cracks are filled as soon as possible, then the concentration is reduced, lime milk with lower concentration easily enters smaller cracks, and fine cracks can be plugged. At the initial set concentration, the plugging can be completed within 10 times of concentration reduction according to the rate reduction of 0.2 times, and the setting is ideal. If the initial set concentration is too low, an integral structure with good plugging performance is not easy to form. However, if the initial set concentration is too high, the lime milk is too thick, and besides the problems of the above and the increase of the concentration reduction times, ports of some cracks are sealed by the thick lime milk, so that the whole annular cement and the size cracks in the surrounding rock breaking zone are not filled, and the sealing effect is also affected.\|[0106] The lowest final set concentration of milk of lime is not lower than the solubility at the temperature of the reservoir 9, which serves to let the milk of lime suspension sufficiently enter the fissures 7 at a set final set pressure (e.g. 1.0 MPa). But the final set concentration must not be below the solution level, otherwise, the subsequent injection of unsaturated lime water will have a damaging effect on the calcium carbonate formed by the reaction of the previously injected lime milk with carbon dioxide.\|[0107] The injection rate described above also affects the occlusion effect. The invention provides a maximum rate limit of 0.5 liter/second at which lime milk entering the crack can react with leaked carbon dioxide in good time to form calcium carbonate to seal the crack. If the speed limit is too high, the blocking effect is not good, but if the speed limit is too low, the blocking is not easy to proceed and the blocking efficiency is too low.\|[0108] The plugging effect monitoring step follows.\|[0109] Monitoring can also be performed by using a gas flow meter provided at the wellhead to measure the gas flow at the wellhead. A wellhead vent valve, which is a valve to a gas flow meter, may also be closed, and the wellhead perimeter carbon dioxide concentration monitored to determine the leak path of carbon dioxide along the abandoned borehole.\|[0110] Alternatively, a monitoring well 13 may be drilled on the side of the well, the well depth of which does not exceed the cap layer 3.\|[0111] Ph value probes (14), an earth surface carbon dioxide concentration meter (15) and a wellhead gas flowmeter (16) are placed in a monitoring well (13) to be matched for use, the Ph value of overlying stratum water, the wellhead periphery carbon dioxide concentration and wellhead carbon dioxide leakage are continuously monitored, and data are analyzed through an earth surface monitoring station (17).\|[0112] The frequency of monitoring may be generally such that data is taken every 12 hours.\|[0113] If no carbon dioxide leakage is found in the 30-day monitoring, the plugging is considered to be successful, and then the following process steps are carried out: and (5) sealing the well.\|[0114] The bridge plug well sealing in the well can be implemented, and the sealing of the leakage of the carbon dioxide along the abandoned well is completed.\|[0115] Firstly, taking out the packer at the upper part of the perforation section, injecting carbon dioxide corrosion resistant cement and the like into the perforation section in the well to form a cement bridge plug for preventing leakage in the well, and integrally completing the plugging of the leakage of carbon dioxide along the abandoned well. The carbon dioxide corrosion resistant cement can be slag cement, volcanic ash cement, fly ash cement or composite cement, etc., and the concrete method of well sealing belongs to the prior art and is not repeated here.\|[0116] If the sealing is not up to standard through monitoring, the leakage reason needs to be specifically analyzed, if the leakage is still caused by the crack around the drilling well, the perforation 4 can be set at a new position again, lime milk can be refilled, at this time, the concentration of the lime milk can be adjusted, for example, the set concentration is increased, and the lime milk can be refilled. And then monitoring the blocking effect until the blocking reaches the standard.\|[0117] According to the invention, the cover layer is preferably perforated, a shaft with leakage risk, drilling annulus cement and a surrounding rock breaking belt are communicated, a packer is arranged in the shaft, a relatively closed space is formed in a perforation section, lime milk suspension is slowly injected into the perforation section through a fracturing truck, the injection pressure is controlled in the process, the concentration of lime milk is gradually reduced, lime milk in a crack reacts with leaked carbon dioxide to form hardened and compact calcium carbonate, and a carbon dioxide leakage channel is further plugged. The invention can effectively block the crack channel leaked along the abandoned well in the geological carbon dioxide sealing process, and can bond the surrounding rock breaking zone and the crack-containing drilling annular cement into a compact whole, thereby greatly reducing the risk of leakage along the abandoned well in the geological carbon dioxide sealing process. The injected lime milk suspension reacts with the carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, so that the risk of geological environment pollution is extremely low, and the plugging process is safe and environment-friendly.	Family Number\|(96423759)\|96423759\|Object of Invention\|(CN113494265 A)\|( . . . ) well in a carbon dioxide geological storage process , which comprises the steps of perforating a stable cover layer on a carbon dioxide geological storage layer , communicating a shaft with leakage risk , drilling annular cement and a surrounding rock crushing zone , injecting lime milk suspension into a perforating section , enabling the lime milk in a gap to react with leaked carbon dioxide to form hardened compact calcium carbonate , and further blocking a carbon dioxide leakage channel . \|Advantages / Prev. Drawbacks\|(CN113494265B B)\|At present , great project demonstration of carbon capture utilization and sealing is developed in each industry of China , and a foundation is laid for subsequent large - scale carbon dioxide injection . \|(CN113494265 A)\|At present , the research on the sealing technology of leakage along a drilling well in the geological carbon dioxide sequestration process is very limited , and the current situation is not favorable for solving the problem of sudden leakage along a waste drilling well in the geological carbon dioxide sequestration process , so that the development of a great environmental protection project of underground carbon dioxide sequestration is limited to a great extent . \|Independent Claims\|(CN113494265 A)\|1. A method for plugging leakage along abandoned wells in the geological carbon dioxide sequestration process is characterized by comprising the following steps : the method comprises the following steps : ( . . . ) \|	Civil engineering	E21B-033/13\|E21B-033/138		E21B-033/13\|E21B-033/138	E21B-033/13\|E21B-033/138	E21B-033/13\|E21B-033/138			CN119715293\|CN117365368\|CN116906838\|CN117703328\|CN115387755\|CN114086915\|US12560053\|CN117347111B\|CN116771414B\|CN115405255B\|CN114163982B	CN119715293 113979591 WHO=Examiner SELF=N CAT=A\|CN117365368 108075309 WHO=Examiner SELF=N CAT=A\|CN116906838 106902088 WHO=Examiner SELF=N CAT=A\|CN117703328 108903396 WHO=Examiner SELF=N CAT=A\|CN115387755 102721841 WHO=Examiner SELF=N CAT=A\|CN114086915 98867716 WHO=Examiner SELF=N CAT=A\|US12560053 115114287 WHO=Applicant SELF=N\|CN117347111B 108069478 WHO=Examiner SELF=N\|CN116771414B 106534659 WHO=Examiner SELF=N\|CN115405255B 102795999 WHO=Examiner SELF=N\|CN114163982B 99082908 WHO=Examiner SELF=N	CN111622746\|CN110284853\|CN105156066\|CN109577908\|CN106382109\|CN108026766\|CN102144074\|WO200662433\|US5035813	CN111622746 90481716 WHO=Examiner SELF=N CAT=Y\|CN110284853 86162646 WHO=Examiner SELF=N CAT=Y\|CN105156066 71726885 WHO=Examiner SELF=N CAT=Y\|CN109577908 84048491 WHO=Examiner SELF=N CAT=A\|CN106382109 75321301 WHO=Examiner SELF=N CAT=A\|CN108026766 74494517 WHO=Examiner SELF=N CAT=A\|CN102144074 1845506 WHO=Examiner SELF=N CAT=A\|WO200662433 36247452 WHO=Examiner SELF=N CAT=A\|US5035813 35696446 WHO=Examiner SELF=N		WO200662433; CN102144074; CN105156066; CN106382109; CN108026766; CN109577908; CN110284853; CN111622746; US5035813		LAPSED	(CN113494265)\|LAPSED	DEAD	(CN113494265)\|DEAD	(CN113494265)\|LEGAL DETAILS FOR CN113494265\|Actual or expected expiration date=2025-07-18\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2021-07-23\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202110837467\|Application date=2021-07-23\|Standardized application number=2021CN-0837467\|Event publication date=2021-10-12\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN113494265\|Publication stage code=A\|Publication date=2021-10-12\|Standardized publication number=CN113494265\|Event publication date=2021-10-12\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2021-10-29\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2023-05-02\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN113494265\|Publication stage code=B\|Publication date=2023-05-02\|Standardized publication number=CN113494265B\|Event publication date=2023-05-02\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2025-07-18\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee			https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTId3YEhR1wxhj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067606327&ekey=2079&xpn=CN113494265B&kind=B	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=TDcyjbThyfq0YYqkBFXZbbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN113494265)\|CN\|(CN113494265)\|CN	(CN113494265)\|NAME=CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS , COUNTRY=CN\|(CN113494265)\|NAME=CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS , COUNTRY=CN		(CN113494265)\|NAME=CHEN YING;BEIJING BEIXIN-ZHICHENG INTELLECTUAL PROPERTY AGENT CO., LTD. , REG=11100\|(CN113494265)\|NAME=CHEN YING;BEIJING BEIXIN-ZHICHENG INTELLECTUAL PROPERTY AGENT CO., LTD. , REG=11100		(CN113494265)\|NAME=FU LEI\|NAME=MA XIN\|NAME=DIAO YUJIE\|NAME=ZHANG CHENGLONG\|NAME=LIU TING\|NAME=Fu Jie\|NAME=SHAO WEI\|(CN113494265)\|NAME=FU LEI\|NAME=MA XIN\|NAME=DIAO YUJIE\|NAME=ZHANG CHENGLONG\|NAME=LIU TING\|NAME=Fu Jie\|NAME=SHAO WEI	(CN113494265)\|2	1	1					(CN113494265)\|Number of Claims: NCL=9\|Gazette date: GAZDATE=2023-05-02\|Gazette number: GAZNUM=39-1801\|Number of Pages: NPAGES=13\|Primary examiner: 柳思源\|Primary examiner: Liu Siyuan\|\|(CN113494265)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2021-10-12\|Gazette number: GAZNUM=37-4201\|Number of Pages: NPAGES=13\|Primary examiner: 柳思源\|Primary examiner: Liu Siyuan\|	(CN113494265)\|Previous publication: CN113494265 A 2021-10-12 [CN113494265]	(CN113494265)\|CHINESE (CHI)	(CN113494265B)\|Patent\|(CN113494265)\|Patent	Titre: (CN113494265)\|Plugging method for leakage along abandoned well in carbon dioxide geological storage process Résumé: (CN113494265)\|The invention provides a method for blocking leakage along an abandoned well in the geological storage process of carbon dioxide. The method comprises the following steps that perforating is carried out by adopting a stable cover layer above a geological storage layer of carbon dioxide; a shaft with leakage risk, drilling annular cement and a surrounding rock fracture zone communicate with one another; and lime milk turbid liquid is injected into a perforation interval, so that lime milk in a gap reacts with leaked carbon dioxide to form hardened and compact calcium carbonate, and a carbon dioxide leakage channel is blocked. According to the method for blocking leakage along the abandoned well in the geological storage process of carbon dioxide, the crack channel leaking along the abandoned well in the geological storage process of carbon dioxide can be effectively blocked, meanwhile, a surrounding rock broken zone and crack-containing drilling well annulus cement can be cemented into a compact whole, and the risk of leaking along the abandoned well in the geological storage process of carbon dioxide is greatly reduced. The injected lime milk turbid liquid reacts with carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, the geological environment pollution risk is extremely low, and the plugging process is safe and environmentally friendly.	36	Abstract	gpt-4o-mini	no	The article focuses on a method for blocking CO₂ leakage in geological storage, not on accelerating mineral weathering or carbon sequestration through enhanced weathering processes.
37	CN202310241385	CN202310241385	CN116359471	105563865	CN116359471 A 2023-06-30 [CN116359471]	2023-03-09	2023-03-09	2023-06-30		(CN116359471)\|2043-03-09	(CN116359471)\|System and method for dynamically simulating mineralized sealed carbon dioxide filled goaf	(CN116359471)\|The invention discloses a system and method for dynamically simulating mineralized sealed carbon dioxide filled goaf, and belongs to the technical field of mineralized sealed carbon dioxide. The device is provided with a mineralization reaction device, a transportation device and a mineralization simulation device, the mineralization reaction device is composed of a reaction main body, an ultrasonic generation device and a bubble generation device, the transportation device is provided with a transportation pipeline and a pipeline monitoring device, and the mineralization simulation device comprises a triaxial loading device and a heating device. The triaxial loading equipment is provided with a material supporting part and a loading assembly. The mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline connector of the transportation device, so that the mineralization reaction system is formed, then the mineralization sealed carbon dioxide filling goaf is dynamically simulated through the mineralization reaction system, and the method is simple and convenient in simulation operation, economical and feasible and conforms to the concept of green mining.	ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY\|SHANDONG UNIVERSITY OF SCIENCE & TECHNOLOGY	(CN116359471)\|ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN])\|SHANDONG UNIVERSITY OF SCIENCE & TECHNOLOGY	WANG CHANGXIANG\|LU YAO\|ZHOU YONGQIANG\|LU WEI\|LI JINLIANG\|LI JINHU\|ZHUO HUI\|ZHANG QINGSONG\|ZHAO SHUJIE\|LI QINGHAI\|SI LEILEI\|JIANG NING	(CN116359471)\|WANG CHANGXIANG\|LU YAO\|ZHOU YONGQIANG\|LU WEI\|LI JINLIANG\|LI JINHU\|ZHUO HUI\|ZHANG QINGSONG\|ZHAO SHUJIE\|LI QINGHAI\|SI LEILEI\|JIANG NING	(CN116359471)\|LONG JUNBO;WEIHAI HENG YU RUN DA PATENT AGENCY OFFICE (GENERAL PARTNERSHIP)\|Reg. Nb: 37260	(CN116359471)\|Carbon dioxide emission and effective treatment are the key problems of attention in various fields, and the proposal of carbon dioxide mineralization sealing gives a solution thought, wherein the carbon dioxide mineralization sealing mainly imitates and accelerates the process of rock weathering and carbon dioxide absorption in nature, carbon dioxide is dissolved in water to generate carbonic acid, then the carbonic acid reacts with alkaline minerals to generate stable solid carbonate, and the stable solid carbonate can not be decomposed in long geological years, so that the permanent sealing of the carbon dioxide can be realized. Because the carbon emission proportion in the coal mine industry is higher, a certain carbon fixation measure is necessary for the coal mine industry, and the mining of coal resources can cause rock stratum movement and ground surface damage, so that goafs need to be filled; the large-scale experiment is limited in site, so that the mineralization filling process of the goaf is simulated in a laboratory in a simulation mode, the practical production significance is great according to the experimental result, the mode is convenient, the economy and the feasibility are realized, and the idea of green exploitation is met.\|	(CN116359471)\|1. A system for dynamically simulating mineralization and sequestration of carbon dioxide filling goaf, comprising: the mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment; the conveying device is provided with a conveying pipeline and a pipeline monitoring device; the mineralization simulation device comprises a triaxial loading device and a heating device, wherein the triaxial loading device is provided with a material supporting part and a loading assembly.\|	(CN116359471)\|The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|The invention discloses a system and a method for dynamically simulating mineralization and carbon dioxide sealing and filling goaf, which belong to the technical field of mineralization and carbon dioxide sealing; the device comprises a mineralization reaction device, a transportation device and a mineralization simulation device, wherein the mineralization reaction device consists of a reaction main body, ultrasonic generating equipment and bubble generating equipment, the transportation device is provided with a transportation pipeline and a pipeline monitoring device, the mineralization simulation device comprises a triaxial loading equipment and a heating equipment, and the triaxial loading equipment is provided with a material supporting part and a loading assembly.\|The invention provides a system for dynamically simulating mineralization to seal carbon dioxide to fill a goaf, aiming at the technical problems in the prior art.\|	(CN116359471)\|CARBON DIOXIDE(100,81)\|SIMULATING MINERALIZATION(100,12)\|FILLING GOAF(100,3)\|CARBON DIOXIDE FILLING GOAF(100,1)\|SEQUESTRATION(100,1)\|MINERALIZATION SIMULATION(66,32)\|MINERALIZATION REACTION(44,49)\|COAL RESOURCE MINING(41,1)\|GREEN EXPLOITATION IDEA(37,1)\|MINERALIZATION SIMULATION AIRTIGHTNESS(33,3)\|COAL MINE INDUSTRY(29,2)\|TRIAXIAL LOADING(28,28)\|GOAF(27,22)\|TRIAXIAL LOADING EQUIPMENT(26,4)\|CONVEYING PIPELINE(25,6)\|MINERALIZATION SEALING(25,1)\|MINERALIZE SIMULATION(25,1)\|TRANSPORTATION PIPELINE(24,4)\|COAL RESOURCE(24,1)\|MINERALIZE PARTY(22,1)\|PASTE FILLING(21,31)\|GENERATING ULTRASOUND EQUIPMENT(20,3)\|CARBON DIOXIDE SEALING(20,2)\|ALKALINE MINERAL(20,1)\|MINERALIZATION(19,17)\|GREEN EXPLOITATION(18,3)\|STABLE SOLID CARBONATE(18,2)\|CARBON DIOXIDE MINERALIZATION SEALING(18,1)\|PRODUCTION SIGNIFICANCE(18,1)\|CARBON DIOXIDE SEQUESTRATION(17,2)\|LONG GEOLOGICAL YEAR(17,1)\|BUBBLE(16,20)\|HEATING EQUIPMENT(16,5)\|SIMULATION MODE(15,1)\|REACTION TANK(14,32)\|REACTION MAIN(14,7)\|FEASIBILITY(14,1)\|PASTE SLUMP(13,4)\|CARBON DIOXIDE MINERALIZATION(13,2)\|STABLE SOLID(13,2)\|CARBON EMISSION PROPORTION(13,1)\|ROCK STRATUM MOVEMENT(13,1)\|SOLUTION THOUGHT(13,1)\|ELECTROMAGNETIC FLOWMETER(12,10)\|CARBIDE SLAG(12,4)\|GOAF STRESS CONDITION(12,2)\|CARBON DIOXIDE ABSORPTION(12,1)\|CARBON DIOXIDE EMISSION(12,1)\|ECONOMY(12,1)\|LABORATORY(12,1)\|MEASURING CARBON FIXATION(12,1)\|LOADING BAFFLE(11,5)\|LOADING EQUIPMENT(11,4)\|CARBONIC ACID(11,2)\|GOAFS(11,1)\|SAMPLING PORT(10,2)\|CARBON DIOXIDE FILLED GOAF(10,1)\|CONVERSION EQUIPMENT(10,1)\|GAS OUTLET(9,10)\|CARBON DIOXIDE CONTENT(9,9)\|MINERALIZE REACTION MATERIAL(9,2)\|ROCK(9,1)\|CARBON DIOXIDE(8,2)\|DETECTION SENSOR(8,2)\|MONITORING EQUIPMENT(8,2)\|CARBON FIXATION(8,1)\|AQUEOUS SOLUTION(7,12)\|GAS SAMPLE(7,5)\|CARBON DIOXIDE BUBBLE(7,3)\|CONVEYING CONDITION(7,3)\|GOAF AREA(7,2)\|MINERALIZATION SIMULATOR(7,2)\|TRANSPORTATION DEVICE(6,16)\|ULTRASOUND(6,11)\|MICRO BUBBLE GENERATOR(6,8)\|ULTRASONIC GENERATING(6,7)\|GANGUE(6,4)\|MONITORING DATA(6,2)\|TRIAXIAL LOADING EXPERIMENT(6,2)\|FILLING PUMP(5,6)\|FLY ASH(5,4)\|GOAF MINERALIZATION AREA(5,4)\|DATA COLLECTION(5,3)\|LAYERING CHANGE VALUE(5,2)\|GROUND SURFACE DAMAGE(5,1)\|LARGE SCALE EXPERIMENT(5,1)\|MINERALIZATION REACTION TEST BLOCK(4,6)\|AIRTIGHTNESS(4,4)\|CARBON DIOXIDE GAS CYLINDER(4,4)\|ENVIRONMENT TEMPERATURE(4,4)\|NACL(4,4)\|TEMPERATURE COLLECTING DATA(4,3)\|COAGULATED TEST INTERNAL BUBBLE(4,2)\|EXPERIMENTAL TOOL(4,2)\|PASTE LAYERING CHANGE(4,2)\|REACTION SOLIDIFICATION(4,2)\|SILICA FUME(4,2)\|SIMULATED FLUE GAS PROPORTIONING(4,2)\|TRIAXIAL LOADING SLOT(4,2)\|ULTRASONIC WAVE CAVITATION(4,2)\|AFTER TRIAXIAL LOADING TEST(4,1)\|CONTENT NUMERIC VALUE CHANGE(4,1)\|ELECTROMETHOD INSTRUMENT(4,1)\|GOAF MINERALIZATION REGION(4,1)\|MINERALIZATION LOADING EXPERIMENT(4,1)\|TRIAXIAL LOADING GROOVING HEAD(4,1)\|TRIAXIAL LOADING NOTCH(4,1)\|SEALING(3,14)\|INTELLIGENT CONTROL(3,11)\|MATERIAL SAMPLING(3,9)\|PIEZORESISTIVE PRESSURE SENSOR(3,8)\|SENSOR INTERFACE(3,5)\|ULTRASONIC TRANSDUCER(3,4)\|BUBBLE GENERATION EQUIPMENT(3,2)\|CETYLTRIMETHYLAMMONIUM BROMIDE(3,2)\|COAGULATION TEST(3,2)\|DATA ACQUISITION(3,2)\|FILLING SITE(3,2)\|GAS TIGHTNESS(3,2)\|NEGLIGIBLE CONTENT(3,2)\|POSITIONAL RELATIONSHIP(3,2)\|SIMULATION EXPERIMENT(3,1)\|GAS COMPONENT ANALYSIS(2,5)\|LOAD PRESSURE HEAD(2,4)\|LOADING PLATE(2,4)\|PLACING MATERIAL AREA(2,4)\|WATER GLASS(2,4)\|MATERIAL TRANSPORTATION PIPELINE(2,3)\|PIPELINE TRANSPORTATION(2,3)\|CTABS(2,2)\|ELECTRICAL TOOL(2,2)\|FILLING VOLUME(2,2)\|FLOWMETER(2,2)\|GAS REACTION(2,2)\|BUBBLE STABILITY(2,1)\|CARBON DIOXIDE MICROBUBBLE(2,1)\|FOAM STABILIZER(2,1)\|GROOVE DIMENSION(2,1)\|IMMOBILIZED(2,1)\|INTENSIFICATION(2,1)\|LOADING GROOVING PRESS HEAD(2,1)\|LOADING STRESS(2,1)\|MICRO NANO BUBBLE MODE(2,1)\|MINERALIZATION REACTION TEST PROPORTION(2,1)\|MINERALIZE REACTION TESTTHE BLOCK(2,1)\|SYMBOL MARK(2,1)\|	(CN116359471)\|1. A system for dynamically simulating mineralization and sequestration of carbon dioxide filling goaf, comprising:\|the mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment;\|the conveying device is provided with a conveying pipeline and a pipeline monitoring device;\|the mineralization simulation device comprises a triaxial loading device and a heating device, wherein the triaxial loading device is provided with a material supporting part and a loading assembly.\|2. The system for dynamically simulating mineralization and sealing of carbon dioxide filling goaf according to claim 1, wherein the reaction main body is provided with a reaction tank, a stirring device is arranged in the reaction tank, the ultrasonic generating equipment is connected with the reaction tank through a conversion equipment, and a carbon dioxide gas cylinder is connected to the bubble generating equipment.\|3. The system for dynamically simulating mineralization, sealing and carbon dioxide filling of goaf according to claim 1, wherein the mineralization simulation device comprises a maintenance part, a loading part and a forming part, the loading part is provided with a material placing area, the peripheral side of the material placing area is provided with a loading pressure head and a loading baffle, and the heating equipment arranged on the forming part is arranged on the lower side of the loading part.\|4. A method for dynamically simulating mineralization and sequestration of carbon dioxide to fill goaf, characterized in that it uses the system for dynamically simulating mineralization and sequestration of carbon dioxide to fill goaf according to any one of claims 1-3, said method comprising the following steps:\|weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|adding water into the bubble generating equipment, then introducing carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into the mineralization reaction device for mineralization reaction;\|conveying the fully mixed mineralized filling paste through the conveying device, collecting data of temperature and pressure in the system, sampling and analyzing the filling paste at an output port through a sampling port, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through the pipeline monitoring device;\|the conveyed mineralized filling paste is conveyed into the mineralization simulation device through a conveying pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and then the mineralized material is naturally cured until the mineralized material is completely solidified;\|at the moment, a triaxial loading test is carried out, a stress condition of the goaf is simulated through triaxial loading equipment, a test block is loaded, and the temperature of a mineralized area of the goaf is simulated through changing the forming environment temperature of the test block through heating equipment;\|after the loading test is finished, extracting gas through the gas outlet hole, carrying out secondary gas component analysis, and comparing an analysis result with a primary component analysis result;\|and finally, completely extracting the gas in the mineralization simulation device through the gas outlet hole, analyzing the gas components to obtain the content change of carbon dioxide in the gas, and judging the mineralization effect of the mineralized material according to the carbon dioxide content numerical value change.\|5. The method for dynamically simulating mineralizing and sequestering carbon dioxide to fill a goaf according to claim 4, wherein the mineralizing reaction material comprises water glass, fly ash, carbide slag, gangue, naOH, naCl, CTAB, H 2 O 2 。\|6. The method for dynamically simulating mineralizing and sequestering carbon dioxide to fill the goaf according to claim 5, wherein the mineralizing reaction material comprises the following components in percentage by mass: 3:7:3:3.\|7. the method for dynamically simulating mineralized and sealed carbon dioxide filling goaf according to claim 4, wherein the mineralized reaction device is connected with the mineralized simulation device through the transportation device to form a test system, and the test system is further provided with an intelligent control system for intelligent control and data monitoring.\|8. The method for dynamically simulating mineralized and sealed carbon dioxide filled goaf according to claim 4, wherein when the mineralized and filled paste is conveyed by the conveying device, data acquisition is carried out on monitoring equipment in the pipeline monitoring device and the mineralization reaction device once every 1 minute, sampling analysis is carried out on the filled paste at an output port of the conveying device every 5 minutes, and analysis on paste slump and paste layering change values is carried out on samples.\|9. The method for dynamically simulating mineralizing, sequestering and carbon dioxide filling a goaf according to claim 4, wherein the temperature and pressure in the system are monitored by the detection sensor when the mineralizing simulation device is heated by the heating equipment in a triaxial loading test, and the mineralizing party is considered to be finished when the pressure in the device is kept unchanged for a long time.\|10. The method for dynamically simulating mineralized and sealed carbon dioxide filling goaf according to claim 4, wherein the content of carbon dioxide fixed by bubbles in the test block after triaxial loading test can be obtained according to the known total amount of the carbon dioxide gas cylinder, the content of carbon dioxide introduced into the system and the content of carbon dioxide theoretically absorbed by the mineralized reaction material, and the mineralized effect of the mineralized material can be judged by the value.	(CN116359471)\|TECHNICAL FIELD\|[0001] The invention belongs to the technical field of mineralized and sealed carbon dioxide, and particularly relates to a system and a method for dynamically simulating mineralized and sealed carbon dioxide to fill a goaf.\|BACKGROUND ART\|[0002] Carbon dioxide emission and effective treatment are the key problems of attention in various fields, and the proposal of carbon dioxide mineralization sealing gives a solution thought, wherein the carbon dioxide mineralization sealing mainly imitates and accelerates the process of rock weathering and carbon dioxide absorption in nature, carbon dioxide is dissolved in water to generate carbonic acid, then the carbonic acid reacts with alkaline minerals to generate stable solid carbonate, and the stable solid carbonate can not be decomposed in long geological years, so that the permanent sealing of the carbon dioxide can be realized.\|[0003] Because the carbon emission proportion in the coal mine industry is higher, a certain carbon fixation measure is necessary for the coal mine industry, and the mining of coal resources can cause rock stratum movement and ground surface damage, so that goafs need to be filled; the large-scale experiment is limited in site, so that the mineralization filling process of the goaf is simulated in a laboratory in a simulation mode, the practical production significance is great according to the experimental result, the mode is convenient, the economy and the feasibility are realized, and the idea of green exploitation is met.\|DISCLOSURE\|Disclosure of Invention\|[0004] The invention provides a system for dynamically simulating mineralization to seal carbon dioxide to fill a goaf, aiming at the technical problems in the prior art.\|[0005] In order to solve the technical problems, the invention comprises:\|[0006] the mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment;\|[0007] the conveying device is provided with a conveying pipeline and a pipeline monitoring device;\|[0008] and the mineralization simulation device comprises a triaxial loading device and a heating device, wherein the triaxial loading device is provided with a material supporting part and a loading assembly.\|[0009] Preferably, the reaction main body is provided with a reaction tank, a stirring device is arranged in the reaction tank, the ultrasonic generating equipment is connected with the reaction tank through a conversion device, and the bubble generating equipment is connected with a carbon dioxide gas cylinder.\|[0010] Preferably, the mineralization simulation device comprises a curing part, a loading part and a forming part, wherein the loading part is provided with a material placing area, the periphery side of the material placing area is provided with a loading pressure head and a loading baffle, and the heating equipment arranged on the forming part is arranged at the lower side of the loading part.\|[0011] The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|[0012] weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|[0013] adding water into bubble generating equipment, then introducing carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into a mineralization reaction device for mineralization reaction;\|[0014] conveying the fully mixed mineralized filling paste through a conveying device, collecting data of temperature and pressure in a system, sampling and analyzing the filling paste at an output port through a sampling port, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through a pipeline monitoring device;\|[0015] the conveyed mineralized filling paste is conveyed into a mineralization simulation device through a conveying pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and then the mineralized material is naturally cured until the mineralized material is completely solidified;\|[0016] at the moment, a triaxial loading test is carried out, a stress condition of the goaf is simulated through triaxial loading equipment, a forming environment temperature of the test block is changed through heating equipment, and the temperature of a mineralized area of the goaf is simulated;\|[0017] after the loading test is finished, extracting gas through the gas outlet hole, carrying out secondary gas component analysis, and comparing an analysis result with a primary component analysis result;\|[0018] and finally, completely extracting the gas in the mineralization simulation device through the gas outlet, analyzing the gas components to obtain the content change of carbon dioxide in the gas, and judging the mineralization effect of the mineralized material according to the numerical value change of the carbon dioxide content.\|[0019] Preferably, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 。\|[0020] Preferably, the mineralization reaction material comprises the following components in percentage by mass: 3:7:3:3.\|[0021] preferably, the mineralization reaction device is connected with the mineralization simulation device through the transportation device to form a test system, and the test system is also provided with an intelligent control system for intelligent control and data monitoring.\|[0022] Preferably, when the mineralized filling paste is conveyed by the conveying device, data acquisition is carried out on the pipeline monitoring device and monitoring equipment in the mineralization reaction device every 1 minute, sampling analysis is carried out on the filling paste at the output port of the conveying device every 5 minutes, and analysis on paste slump and paste layering change values is carried out on samples.\|[0023] Preferably, when a triaxial loading test is performed, the mineralization simulation device is heated by the heating equipment, the temperature and the pressure in the system are monitored by the detection sensor, and the mineralization is considered to be finished when the pressure in the device is kept unchanged for a long time.\|[0024] Preferably, the content of carbon dioxide fixed by bubbles in the test block after the triaxial loading test can be obtained according to the known total amount in the carbon dioxide cylinder, the content of carbon dioxide introduced into the system and the content of carbon dioxide theoretically absorbed by the mineralization reaction material, and the mineralization effect of the mineralization material can be judged according to the value.\|[0025] Compared with the prior art, the invention has the following beneficial effects:\|[0026] the invention has simple and convenient simulation operation, is economical and feasible, and accords with the concept of green exploitation; by adding foaming agents such as hydrogen peroxide, aluminum powder, silica fume and the like into the mineralized reaction material, the void ratio of the mineralized material after complete reaction solidification is improved, and the filling volume is enlarged; the method comprises the steps of generating an aqueous solution containing micro-nano carbon dioxide bubbles by a micro-nano bubble generating device from carbon dioxide gas and water, introducing a mineralization reaction material to promote mineralization reaction, improving mineralization reaction rate, combining mechanical stirring and ultrasonic waves, and promoting mineralization reaction by using cavitation of ultrasonic waves and mechanical stirring.\|[0027] The transportation device adopts a sectional type transportation pipeline to simulate the transportation of mineralized filling paste on a filling site, the mineralization simulation device simulates the stress condition of a goaf to load a mineralization reaction test block, the heating device changes the temperature of the test block to simulate the temperature of a mineralization area of the goaf, and the triaxial loading device performs triaxial loading experiments on the test block in the mineralization simulation device according to the stress condition of the filling goaf, so that the test environment is ensured to be more attached to a real operation environment, and the simulation result is feasible and effective; by analyzing the gas after loading, the aim of detecting whether the mineralized filling paste can realize goaf filling is fulfilled.\|DRAWINGS DESCRIPTION\|[0028] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are required for the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0029] FIG. 1 is a schematic structural view of a mineralization reaction device according to the present invention;\|[0030] FIG. 2 is a schematic view of a transportation device according to the present invention;\|[0031] FIG. 3 is a schematic top view of the mineralization simulator of the present invention;\|[0032] FIG. 4 is a schematic diagram of the front view of the mineralization simulator of the present invention.\|[0033] The symbol marks in the figures illustrate:\|[0034] 1. a reaction tank; 2. a mechanical stirring device; 3. a carbon dioxide microbubble generator; 4. a gas cylinder; 5. a gas control valve; 6. a flow meter; 7. an ultrasonic wave generating device; 8. an ultrasonic transducer; 9. a pressure sensor; 10. a temperature sensor; 11. a filling pump; 12. paste filling pipeline; 13. a delivery control valve; 14. mineralized material transport pipelines; 15. an electromagnetic flowmeter; 16. a piezoresistive pressure sensor; 17. a mineralized material sampling port; 18. a device body; 19. a material placement area; 20. a triaxial loading device; 21. loading an original pressure head by a triaxial; 22. triaxial loading grooving press heads; 23. loading a baffle; 24. an electric heating plate; 25. an electric hot plate controller; 26. sealing cover; 27. an air outlet hole; 28. a sensor interface; 29. an electrical method instrument.\|INVENTION MODE\|Detailed Description\|[0035] In order to make the technical problems, technical schemes and beneficial effects to be solved by the present application more clear, the present application is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the present application.\|[0036] Referring to fig. 1, the invention provides a system for dynamically simulating mineralization, sealing and carbon dioxide filling goaf, which comprises a mineralization reaction device, a transportation device and a mineralization simulation device, wherein the mineralization reaction device is connected with the mineralization simulation device through the transportation device to form a test system, and the test system is also provided with an intelligent control system, so that intelligent control and data monitoring of the system can be performed through the intelligent control system.\|[0037] The mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment.\|[0038] Specifically, the reaction main body is provided with a reaction tank 1 for mineralizing reaction materials; a mechanical stirring device 2 is arranged in the reaction tank 1, and the mineralization reaction can be promoted to be carried out through the mechanical stirring device 2; the upper end of the reaction tank 1 is connected with bubble generating equipment arranged at the outer end through a connecting pipeline, the bubble generating equipment comprises a carbon dioxide micro-bubble generator 3 and a gas cylinder 4, the gas cylinder 4 is connected to the carbon dioxide micro-bubble generator 3, and carbon dioxide is injected into the carbon dioxide micro-bubble generator 3 through the gas cylinder 4.\|[0039] Furthermore, the bubble generating equipment is also provided with a flowmeter 6 and a gas control valve 5, and the flowmeter 6 and the gas control valve 5 are arranged on a connecting pipeline connected with the outer end of the bubble generating equipment; the bubble generating device is used for improving the mineralization reaction efficiency by introducing carbon dioxide and water into the mineralization reaction device in a micro-nano bubble mode.\|[0040] As shown in fig. 1, the lower end of the reaction tank 1 is connected with an ultrasonic generating device through a connecting line, the ultrasonic generating device comprises an ultrasonic generating device 7 and an ultrasonic transducer 8, the ultrasonic transducer 8 is fixedly arranged at the bottom of the reaction tank 1, the ultrasonic generating device 7 is connected with the reaction tank 1 through the ultrasonic transducer 8, the power of ultrasonic waves can be controlled through the ultrasonic generating device 7, the mineralization effect can be improved, and the mineralization of carbon dioxide is promoted.\|[0041] Still further, the ultrasonic wave generating means 7 may be an ultrasonic wave generator or other ultrasonic wave generating device.\|[0042] Furthermore, a pressure sensor 9 and a temperature sensor 10 are also connected to the reaction tank 1 for monitoring the reaction pressure and the reaction temperature in the reaction tank 1.\|[0043] The reaction tank 1 is provided with a mineralization reaction material conveying port through which mineralization reaction materials can be added into the reaction tank 1; the bottom end of the reaction tank 1 is connected with a filling pump 11 and a paste filling pipeline 12, so that mineralized filling paste after being fully mixed is conveyed to a conveying device for conveying through the paste filling pipeline 12, and a conveying control valve 13 is arranged on the paste filling pipeline 12 and used for controlling the conveying of the mineralized filling paste.\|[0044] As shown in fig. 2, the transportation device comprises a plurality of sectional detachable connection type mineralized material transportation pipelines 14, an electromagnetic flowmeter 15 and a piezoresistive pressure sensor 16, wherein the electromagnetic flowmeter 15 is arranged at the inlet of the mineralized material transportation pipelines 14, and a mineralized material sampling port 17 is arranged at the outlet of the mineralized material transportation pipelines 14, so that sampling and monitoring are facilitated. The transportation device simulates the pipeline transportation of mineralized materials in a mineralized filling site, and the flow condition of the mineralized materials in the pipeline is monitored in real time through the electromagnetic flowmeter 15 and the piezoresistive pressure sensor 16.\|[0045] Further, a plurality of piezoresistive pressure sensors 16 are provided at a certain distance from each other inside the mineralized material transporting pipe 14 for pressure monitoring of the paste material transported in the pipe.\|[0046] As shown in fig. 3 and 4, the mineralization simulation device is an integrated treatment device for curing, molding and loading mineralization reaction materials, and comprises a curing part, a loading part and a molding part, wherein the curing part, the loading part and the molding part are all arranged in the device main body 18; the curing part is arranged in the loading part, and when the loading test is not performed, the curing part is used for performing natural curing of the mineralized material, and the loading part is used for performing a triaxial loading test of the mineralized material.\|[0047] Specifically, the curing part is a material placing area 19 arranged at the inner side of the loading part and used for placing mineralized materials for curing and loading test; the loading part is provided with a triaxial loading device 20, the compression strength of the sample after the mineralized material is loaded, analyzed and mineralized by the triaxial loading device 20, the triaxial loading device 20 comprises a triaxial loading original pressure head 21, a triaxial loading slotted pressure head 22, a loading baffle plate 23 and an electrical instrument 29, the triaxial loading slotted pressure head 22 is arranged at the inner end of the triaxial loading original pressure head 21 and is connected through threads, and the loading pressure head and the loading baffle plate 23 are arranged at the outer peripheral side of the material placing area 19.\|[0048] The shaping portion includes electric plate 24 and electric plate controller 25, and shaping portion sets up in the below of triaxial loading device 20, heats up mineralization analogue means through the electric plate 24 of shaping portion, detects temperature change through temperature sensor after the intensification, adjusts the scope of control mineralization analogue means inside temperature to the heating element, can also change the shaping ambient temperature of test block through electric plate 24 and simulate the temperature in goaf mineralization region moreover.\|[0049] Further, as a preferred embodiment of the present invention, the electric heating plate 24 is a constant temperature graphite electric heating plate.\|[0050] Further, as a preferred embodiment of the present invention, the loading plate 23 is disposed at the inner end of the triaxial loading slot die 22, the loading plate 23 has a square plate structure, and the triaxial loading slot die 22 can abut against the loading plate 23, so that a loading force can be applied to the sample placed in the material placement region 19; and the triaxial loading device 20 is provided with a plurality of groups of loading pressure heads and loading baffles 23 which are connected in a matched manner, so that triaxial loading tests can be carried out on the samples.\|[0051] Further, the loading baffle 23 is divided into an upper part and a lower part, the lower loading baffle is arranged on the base at the lower end, and the upper loading baffle and the lower loading baffle are connected with two ends of the notch of the triaxial loading slotting pressure head 22 through threads; the triaxial loading grooving head 22 is provided with a variety of grooving dimensions, the angle being variable, and the shape and size of the loading plate 23 being variable, so as to accommodate variations in the size and inclination of the mineralised reaction material.\|[0052] Specifically, as shown in fig. 4, the upper end of the device main body 18 is further provided with a sealing cover 26 for sealing the device, so as to ensure the air tightness of the device; the sealing cover 26 is provided with an air outlet 27 and a sensor interface 28, the air inside the device is sampled and detected through the air outlet 27, the bubble stability of the mineralized sample can be judged through detection, and the sensor interface 28 can be used for connecting a temperature sensor and a pressure sensor for temperature and pressure monitoring and controlling the loading process through an electromethod instrument 29.\|[0053] Furthermore, before closing the sealing cover 26, high vacuum silicone grease is applied to the contact surface between the sealing cover 26 and the loading part arranged at the lower side to ensure the air tightness of the device.\|[0054] Example 1\|[0055] The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|[0056] step 1: the mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline joint of the transportation device, so that a mineralization reaction system is formed.\|[0057] Step 2: the mineralized reaction material is weighed and prepared, and is filled into a mineralized reaction device.\|[0058] Specifically, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 The composition and the optimal proportion of each part of mineralization reaction material are shown in the following table.\|[0059] TABLE 1 mineralization reaction materials composition materials and proportion table thereof\|[0060] \|[0061] The CTABs listed in table 1 are cetyltrimethylammonium bromide.\|[0062] Specifically, the filling pump 11 and the delivery control valve 13 at the bottom end of the reaction tank 1 are closed, and the prepared mineralized reaction material is added into the reaction tank 1 through the mineralized reaction material delivery port.\|[0063] Step 3: opening a gas control valve 5 and a carbon dioxide micro-bubble generator 3 of the bubble generating equipment, firstly adding a certain amount of water into the carbon dioxide micro-bubble generator 3, then introducing carbon dioxide in a gas cylinder 4 into the carbon dioxide micro-bubble generator 3, generating an aqueous solution containing micro-nano carbon dioxide bubbles through the device, and then introducing the aqueous solution into a reaction tank 1 to start mineralization reaction; the mechanical stirring device 2 and the ultrasonic generating device 7 arranged in the reaction tank 1 are opened to improve the mineralization reaction efficiency of the reaction tank 1.\|[0064] After the mineralized reaction material and carbon dioxide in the reaction tank 1 fully react, a filling pump 11 and a conveying control valve 13 connected with the bottom end of the reaction tank 1 are opened, and the fully mixed mineralized reaction material is conveyed to a mineralization simulation device in a paste form through a paste filling pipeline 12 by a conveying device.\|[0065] Step 4: a piezoresistive pressure sensor 16, an electromagnetic flowmeter 15 and a mineralized material sampling port 17 in the transportation device are opened, and the transportation condition of mineralized filling paste in a transportation pipeline is observed; because the system is provided with the intelligent control system, the intelligent control system is utilized to collect data online, the pressure sensor, the temperature sensor and the electromagnetic flowmeter 15 in each experimental process collect data once every 60 seconds, and the filling paste at the output port of the conveying device is sampled and analyzed through the mineralized material sampling port every 5 minutes.\|[0066] Specifically, whether the filled paste can be transported smoothly in the pipeline without blocking the pipeline is judged by analyzing the data of the pressure sensor, the temperature sensor and the electromagnetic flowmeter, and whether the filled paste still can meet the paste pumping requirement after long-time pipeline transportation is judged by analyzing the paste slump and the paste layering change value of the sample of the mineralized material sampling port 17; the transportation condition of the filling paste in the pipeline is monitored in real time through the piezoresistive pressure sensor 16 and the sampling port to observe whether the mineralized filling paste can be transported smoothly.\|[0067] Step 5: opening a sealing cover 26 on the triaxial loading device 20, conveying the conveyed mineralized filling paste to a material placing area 19 in the mineralized simulation device through a conveying pipeline, and then closing the sealing cover 26 to ensure the air tightness in the device; the gas is sampled for the first time through the gas outlet 27 on the device main body 18, the sampled gas is subjected to component analysis through an experimental instrument, analysis data are recorded, and then the gas outlet 27 is closed to ensure the gas tightness of the device.\|[0068] The mineralized material is naturally cured for 12 hours, after 12 hours, the test block is completely solidified, and then a triaxial loading test can be carried out.\|[0069] Step 6: opening the sensor interface 28, and observing the change of the temperature and the pressure inside the device through the temperature and the pressure sensor; loading a mineralization reaction test block by simulating the stress condition of the goaf through a mineralization simulation device, and changing the temperature of the test block through an electric heating plate 24 of a forming part to simulate the temperature of a mineralization area of the goaf; the test block is subjected to a triaxial loading experiment according to the stress condition of the filled goaf by the triaxial loading device 20, and the forming environment temperature of the mineralized sample is changed by the electric heating plate 24.\|[0070] Step 7: when the sensor detects that the pressure in the device is kept unchanged for a long time, the mineralization reaction is finished, the air outlet 27 is opened to extract the air, the air in the device is collected for the second time, the analysis of the second air component is carried out, and the analysis result is compared with the analysis result of the first component;\|[0071] the existence condition of the internal bubbles of the coagulated test block after triaxial loading test with certain strength can be judged through comparison of the two groups of data, a part of bubbles are destroyed after triaxial loading, and the internal carbon dioxide gas is dispersed, so that the gas component of the loading device is changed, and the two gas analyses can be different.\|[0072] Step 8: finally, all the gases in the mineralization simulation device are extracted through the air outlet holes 27, and the gas component analysis is carried out to obtain the content change of carbon dioxide in the gases; according to the known total amount of the carbon dioxide gas cylinder, the content of carbon dioxide gas introduced into the system and the content of carbon dioxide which can be absorbed by the mineralization reaction material in theory, the content of carbon dioxide fixed by bubbles in the test block after the triaxial loading test can be obtained, and the mineralization effect of the mineralization material can be judged by the value.\|[0073] Therefore, the stability of the mineralized carbon dioxide can be verified, the efficiency of the mineralized reaction for absorbing the carbon dioxide can be calculated, and the compressive strength of the mineralized test block can be obtained through the damage condition of the test block after the triaxial loading test, so that whether the mineralized filling material can well fill the goaf can be judged.\|[0074] Example two\|[0075] The embodiment provides a method for dynamically simulating and mineralizing and sealing carbon dioxide in flue gas to fill a goaf, which comprises the following steps:\|[0076] step 1: the mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline joint of the transportation device, so that a mineralization reaction system is formed.\|[0077] Step 2: the mineralized reaction material is weighed and prepared, and is filled into a mineralized reaction device.\|[0078] Specifically, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 The composition and the optimal proportion of each part of mineralization reaction material are shown in the following table.\|[0079] TABLE 1 mineralization reaction materials composition materials and proportion table thereof\|[0080] \|[0081] The CTABs listed in table 1 are cetyltrimethylammonium bromide.\|[0082] Specifically, H 2 O 2 The CATB is a foam stabilizer.\|[0083] Specifically, the filling pump 11 and the delivery control valve 13 at the bottom end of the reaction tank 1 are closed, and the prepared mineralized reaction material is added into the reaction tank 1 through the mineralized reaction material delivery port.\|[0084] Step 3: using dried air and analytically pure CO 2 Proportioning of simulated flue gas, recording CO 2 The percentage of gas was set to a%.\|[0085] Since the composition of conventional fuel gas, fuel oil and coal flue gas is as follows: n (N) 2 :82%~89%,CO 2 :8%~15%,O 2 :3% -5%, a small amount of SO 2 Because of SO 2 The content of (C) is small, and the design is not considered, so that the dried air and pure CO for analysis are utilized 2 The composition of the flue gas can be simulated relatively accurately. (the normal air gas composition is as follows: N 2 :78%,O 2 21 percent of rare gas: 0.939%, CO 2 : 0.031), other gases and impurities: 0.03%).\|[0086] Step 4: opening a gas control valve 5 of a bubble generating device and a carbon dioxide micro-bubble generator 3, firstly adding a certain amount of water into the carbon dioxide micro-bubble generator 3, then introducing proportioned simulated flue gas, recording the total volume of the introduced gas as V, generating an aqueous solution containing micro-nano carbon dioxide bubbles through the device, and then introducing the aqueous solution into a reaction tank 1 to start mineralization reaction; the mechanical stirring device 2 and the ultrasonic generating device 7 arranged in the reaction tank 1 are opened to improve the mineralization reaction efficiency of the reaction tank 1.\|[0087] After the mineralized reaction material and carbon dioxide in the reaction tank 1 fully react, a filling pump 11 and a conveying control valve 13 connected with the bottom end of the reaction tank 1 are opened, and the fully mixed mineralized reaction material is conveyed to a mineralization simulation device in a paste form through a paste filling pipeline 12 by a conveying device.\|[0088] Step 5: a piezoresistive pressure sensor 16, an electromagnetic flowmeter 15 and a mineralized material sampling port 17 in the transportation device are opened, and the transportation condition of mineralized filling paste in a transportation pipeline is observed; because the system is provided with the intelligent control system, the intelligent control system is utilized to collect data online, the pressure sensor, the temperature sensor and the electromagnetic flowmeter 15 in each experimental process collect data once every 60 seconds, and the filling paste at the output port of the conveying device is sampled and analyzed through the mineralized material sampling port every 5 minutes.\|[0089] Specifically, whether the filled paste can be transported smoothly in the pipeline without blocking the pipeline is judged by analyzing the data of the pressure sensor, the temperature sensor and the electromagnetic flowmeter, and whether the filled paste still can meet the paste pumping requirement after long-time pipeline transportation is judged by analyzing the paste slump and the paste layering change value of the sample of the mineralized material sampling port 17; the transportation condition of the filling paste in the pipeline is monitored in real time through the piezoresistive pressure sensor 16 and the sampling port to observe whether the mineralized filling paste can be transported smoothly.\|[0090] Step 6: opening a sealing cover 26 on the triaxial loading device 20, conveying the conveyed mineralized filling paste to a material placing area 19 in the mineralized simulation device through a conveying pipeline, and then closing the sealing cover 26 to ensure the air tightness in the device; the gas is sampled for the first time through the gas outlet 27 on the device main body 18, the sampled gas is subjected to component analysis through an experimental instrument, analysis data are recorded, and then the gas outlet 27 is closed to ensure the gas tightness of the device.\|[0091] Specifically, the CO in the gas is obtained by sampling analysis 2 The proportion of the gas is b percent, and the gas which can chemically react with mineralized reaction materials in the simulated flue gas is mainly CO 2 The other reactive gases are of a smaller and negligible content and therefore can pass through the initial state CO 2 The ratio of the catalyst to the catalyst is a) and the residual CO in the mineralization reaction device after the reaction can be obtained 2 The content is as follows\|[0092] CO consumed by mineralization 2 The content is->\|[0093] And (3) carrying out natural maintenance on the mineralized material, and carrying out a triaxial loading test after the test block is completely solidified.\|[0094] Step 7: opening the sensor interface 28, and observing the change of the temperature and the pressure inside the device through the temperature and the pressure sensor; loading a mineralization reaction test block by simulating the stress condition of the goaf through a mineralization simulation device, and changing the temperature of the test block through an electric heating plate 24 of a forming part to simulate the temperature of a mineralization area of the goaf; the test block is subjected to a triaxial loading experiment according to the stress condition of the filled goaf by the triaxial loading device 20, and the forming environment temperature of the mineralized sample is changed by the electric heating plate 24.\|[0095] Step 8: when the pressure in the device is detected to be unchanged for a long time through the sensor, the mineralization reaction is considered to be finished, after the loading test is finished, the mineralization reaction test block is fully compressed until the gas fixed by bubbles in the test block is completely crushed and completely released, at the moment, the compression strength of the mineralization reaction test block can be obtained through the mineralization loading device, then the gas is extracted through the gas outlet 27, the gas in the device is collected for the second time, the analysis of the gas component for the second time is carried out, and the analysis result of the first component are calculated, so that the pressure-resistant strength of the mineralization reaction test block can be obtainedCO immobilized by bubbles on mineralized reaction test block 2 And (3) gas.\|[0096] The existence condition of the internal bubbles of the coagulated test block after triaxial loading test with certain strength can be judged through comparison of the two groups of data, a part of bubbles are destroyed after triaxial loading, and the internal carbon dioxide gas is dispersed, so that the gas component of the loading device is changed, and the two gas analyses can be different.\|[0097] Step 9: finally, all the gases in the mineralization simulation device are extracted through the air outlet holes 27, and the gas component analysis is carried out to obtain the content change of carbon dioxide in the gases; CO consumed by mineralization 2 Content, CO immobilized by bubbles in mineralized reaction block 2 The mineralization effect of the mineralization material is comprehensively judged by the content and the pressure bearing condition of the mineralization test block.\|[0098] Therefore, the stability of the mineralized carbon dioxide can be verified, the efficiency of the mineralized reaction for absorbing the carbon dioxide can be calculated, and the compressive strength of the mineralized test block can be obtained through the damage condition of the test block after the triaxial loading test, so that whether the mineralized filling material can well fill the goaf can be judged.\|[0099] Example III\|[0100] The embodiment provides a simulation experiment under different stress loading, and the manufacturing process and the proportion of the mineralization reaction test block of the embodiment are guaranteed to be the same as those of the embodiment one, and specifically comprises the following steps:\|[0101] step 1: weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|[0102] step 2: using dried air and analytically pure CO 2 Proportioning of simulated flue gas, recording CO 2 The percentage of the gas is set as a%;\|[0103] step 3: adding water into bubble generation equipment, then introducing proportioned simulated flue gas, recording the total volume of the introduced gas as V carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into a mineralization reaction device for mineralization reaction;\|[0104] step 4: conveying the fully mixed mineralized filling paste through a conveying device, collecting data of temperature and pressure in the system, sampling and analyzing the filling paste at an output port through a mineralized material sampling port 17, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through a pipeline monitoring device;\|[0105] step 5: the transported mineralized filling paste is transported to a mineralization simulation device through a transportation pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and the CO in the gas at the moment is obtained 2 The proportion of the gas is b percent, and the gas which can chemically react with mineralized reaction materials in the simulated flue gas is mainly CO 2 The other reactive gases are of a smaller and negligible content and therefore can pass through the initial state CO 2 The ratio of the catalyst to the catalyst is a) and the residual CO in the mineralization reaction device after the reaction can be obtained 2 The content is as follows:\|[0106] CO consumed by mineralization 2 The content is->\|[0107] And then naturally curing the mineralized material until the mineralized material is completely solidified.\|[0108] Step 6: the specific compressive strength of the test block can be known through the mineralization loading experiment of the first embodiment, the compressive strength is divided stepwise according to the compressive strength obtained in the first embodiment, the compressive strength is loaded step by step from low to high through the electrical instrument 29, and the damage degree of the test block during loading of each stage is obtained through analyzing the gas extracted from the gas outlet hole.\|[0109] Example IV\|[0110] The present example provides a secondary mineralization test under triaxial loading, and the mix ratio of mineralization reaction test blocks is the same as that of example one.\|[0111] In the solidification process of the mineralized reaction test block, simulating the stress condition of filling the goaf to carry out loading experiments on the test block, and introducing enough CO into the device in the loading process 2 Gas to mineralize reaction testThe block is subjected to secondary mineralization in loading, so that the mineralization sealing quantity is increased, the mineralization rate is improved, and the mineralization effect is enhanced.\|[0112] In mineralization reaction test block in CO 2 After the mineralization reaction is completed in the gas environment, the test block is subjected to a loading experiment again after the test block is completely solidified, the compression strength of the test block obtained by the loading experiment is compared with the compression strength of the test block obtained by the first experiment, and the degree of strengthening of the mineralization reaction by secondary mineralization is judged.\|[0113] The invention has simple and convenient simulation operation, is economical and feasible, and accords with the concept of green exploitation; by adding foaming agents such as hydrogen peroxide, aluminum powder, silica fume and the like into the mineralized reaction material, the void ratio of the mineralized material after complete reaction solidification is improved, and the filling volume is enlarged; the method comprises the steps of generating an aqueous solution containing micro-nano carbon dioxide bubbles by a micro-nano bubble generating device from carbon dioxide gas and water, introducing a mineralization reaction material to promote mineralization reaction, improving mineralization reaction rate, combining mechanical stirring and ultrasonic waves, and promoting mineralization reaction by using cavitation of ultrasonic waves and mechanical stirring.\|[0114] The transportation device adopts a sectional type transportation pipeline to simulate the transportation of mineralized filling paste on a filling site, the mineralization simulation device simulates the stress condition of a goaf to load a mineralization reaction test block, the heating device changes the temperature of the test block to simulate the temperature of a mineralization area of the goaf, and the triaxial loading device performs triaxial loading experiments on the test block in the mineralization simulation device according to the stress condition of the filling goaf, so that the test environment is ensured to be more attached to a real operation environment, and the simulation result is feasible and effective; by analyzing the gas after loading, the aim of detecting whether the mineralized filling paste can realize goaf filling is fulfilled.\|[0115] In the description of the present invention, it should be understood that the directions or positional relationships such as the terms "length", "width", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of description and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present application.\|[0116] Furthermore, in the description of the present application, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.\|[0117] The foregoing description of the preferred embodiments of the present application is not intended to be limiting, but is intended to cover any and all modifications, equivalents, and alternatives falling within the spirit and principles of the present application.	(CN116359471)\|TECHNICAL FIELD\|[0001] The invention belongs to the technical field of mineralized and sealed carbon dioxide, and particularly relates to a system and a method for dynamically simulating mineralized and sealed carbon dioxide to fill a goaf.\|BACKGROUND ART\|[0002] Carbon dioxide emission and effective treatment are the key problems of attention in various fields, and the proposal of carbon dioxide mineralization sealing gives a solution thought, wherein the carbon dioxide mineralization sealing mainly imitates and accelerates the process of rock weathering and carbon dioxide absorption in nature, carbon dioxide is dissolved in water to generate carbonic acid, then the carbonic acid reacts with alkaline minerals to generate stable solid carbonate, and the stable solid carbonate can not be decomposed in long geological years, so that the permanent sealing of the carbon dioxide can be realized.\|[0003] Because the carbon emission proportion in the coal mine industry is higher, a certain carbon fixation measure is necessary for the coal mine industry, and the mining of coal resources can cause rock stratum movement and ground surface damage, so that goafs need to be filled; the large-scale experiment is limited in site, so that the mineralization filling process of the goaf is simulated in a laboratory in a simulation mode, the practical production significance is great according to the experimental result, the mode is convenient, the economy and the feasibility are realized, and the idea of green exploitation is met.\|DISCLOSURE\|Disclosure of Invention\|[0004] The invention provides a system for dynamically simulating mineralization to seal carbon dioxide to fill a goaf, aiming at the technical problems in the prior art.\|[0005] In order to solve the technical problems, the invention comprises:\|[0006] the mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment;\|[0007] the conveying device is provided with a conveying pipeline and a pipeline monitoring device;\|[0008] and the mineralization simulation device comprises a triaxial loading device and a heating device, wherein the triaxial loading device is provided with a material supporting part and a loading assembly.\|[0009] Preferably, the reaction main body is provided with a reaction tank, a stirring device is arranged in the reaction tank, the ultrasonic generating equipment is connected with the reaction tank through a conversion device, and the bubble generating equipment is connected with a carbon dioxide gas cylinder.\|[0010] Preferably, the mineralization simulation device comprises a curing part, a loading part and a forming part, wherein the loading part is provided with a material placing area, the periphery side of the material placing area is provided with a loading pressure head and a loading baffle, and the heating equipment arranged on the forming part is arranged at the lower side of the loading part.\|[0011] The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|[0012] weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|[0013] adding water into bubble generating equipment, then introducing carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into a mineralization reaction device for mineralization reaction;\|[0014] conveying the fully mixed mineralized filling paste through a conveying device, collecting data of temperature and pressure in a system, sampling and analyzing the filling paste at an output port through a sampling port, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through a pipeline monitoring device;\|[0015] the conveyed mineralized filling paste is conveyed into a mineralization simulation device through a conveying pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and then the mineralized material is naturally cured until the mineralized material is completely solidified;\|[0016] at the moment, a triaxial loading test is carried out, a stress condition of the goaf is simulated through triaxial loading equipment, a forming environment temperature of the test block is changed through heating equipment, and the temperature of a mineralized area of the goaf is simulated;\|[0017] after the loading test is finished, extracting gas through the gas outlet hole, carrying out secondary gas component analysis, and comparing an analysis result with a primary component analysis result;\|[0018] and finally, completely extracting the gas in the mineralization simulation device through the gas outlet, analyzing the gas components to obtain the content change of carbon dioxide in the gas, and judging the mineralization effect of the mineralized material according to the numerical value change of the carbon dioxide content.\|[0019] Preferably, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 。\|[0020] Preferably, the mineralization reaction material comprises the following components in percentage by mass: 3:7:3:3.\|[0021] preferably, the mineralization reaction device is connected with the mineralization simulation device through the transportation device to form a test system, and the test system is also provided with an intelligent control system for intelligent control and data monitoring.\|[0022] Preferably, when the mineralized filling paste is conveyed by the conveying device, data acquisition is carried out on the pipeline monitoring device and monitoring equipment in the mineralization reaction device every 1 minute, sampling analysis is carried out on the filling paste at the output port of the conveying device every 5 minutes, and analysis on paste slump and paste layering change values is carried out on samples.\|[0023] Preferably, when a triaxial loading test is performed, the mineralization simulation device is heated by the heating equipment, the temperature and the pressure in the system are monitored by the detection sensor, and the mineralization is considered to be finished when the pressure in the device is kept unchanged for a long time.\|[0024] Preferably, the content of carbon dioxide fixed by bubbles in the test block after the triaxial loading test can be obtained according to the known total amount in the carbon dioxide cylinder, the content of carbon dioxide introduced into the system and the content of carbon dioxide theoretically absorbed by the mineralization reaction material, and the mineralization effect of the mineralization material can be judged according to the value.\|[0025] Compared with the prior art, the invention has the following beneficial effects:\|[0026] the invention has simple and convenient simulation operation, is economical and feasible, and accords with the concept of green exploitation; by adding foaming agents such as hydrogen peroxide, aluminum powder, silica fume and the like into the mineralized reaction material, the void ratio of the mineralized material after complete reaction solidification is improved, and the filling volume is enlarged; the method comprises the steps of generating an aqueous solution containing micro-nano carbon dioxide bubbles by a micro-nano bubble generating device from carbon dioxide gas and water, introducing a mineralization reaction material to promote mineralization reaction, improving mineralization reaction rate, combining mechanical stirring and ultrasonic waves, and promoting mineralization reaction by using cavitation of ultrasonic waves and mechanical stirring.\|[0027] The transportation device adopts a sectional type transportation pipeline to simulate the transportation of mineralized filling paste on a filling site, the mineralization simulation device simulates the stress condition of a goaf to load a mineralization reaction test block, the heating device changes the temperature of the test block to simulate the temperature of a mineralization area of the goaf, and the triaxial loading device performs triaxial loading experiments on the test block in the mineralization simulation device according to the stress condition of the filling goaf, so that the test environment is ensured to be more attached to a real operation environment, and the simulation result is feasible and effective; by analyzing the gas after loading, the aim of detecting whether the mineralized filling paste can realize goaf filling is fulfilled.\|DRAWINGS DESCRIPTION\|[0028] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are required for the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0029] FIG. 1 is a schematic structural view of a mineralization reaction device according to the present invention;\|[0030] FIG. 2 is a schematic view of a transportation device according to the present invention;\|[0031] FIG. 3 is a schematic top view of the mineralization simulator of the present invention;\|[0032] FIG. 4 is a schematic diagram of the front view of the mineralization simulator of the present invention.\|[0033] The symbol marks in the figures illustrate:\|[0034] 1. a reaction tank; 2. a mechanical stirring device; 3. a carbon dioxide microbubble generator; 4. a gas cylinder; 5. a gas control valve; 6. a flow meter; 7. an ultrasonic wave generating device; 8. an ultrasonic transducer; 9. a pressure sensor; 10. a temperature sensor; 11. a filling pump; 12. paste filling pipeline; 13. a delivery control valve; 14. mineralized material transport pipelines; 15. an electromagnetic flowmeter; 16. a piezoresistive pressure sensor; 17. a mineralized material sampling port; 18. a device body; 19. a material placement area; 20. a triaxial loading device; 21. loading an original pressure head by a triaxial; 22. triaxial loading grooving press heads; 23. loading a baffle; 24. an electric heating plate; 25. an electric hot plate controller; 26. sealing cover; 27. an air outlet hole; 28. a sensor interface; 29. an electrical method instrument.\|INVENTION MODE\|Detailed Description\|[0035] In order to make the technical problems, technical schemes and beneficial effects to be solved by the present application more clear, the present application is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the present application.\|[0036] Referring to fig. 1, the invention provides a system for dynamically simulating mineralization, sealing and carbon dioxide filling goaf, which comprises a mineralization reaction device, a transportation device and a mineralization simulation device, wherein the mineralization reaction device is connected with the mineralization simulation device through the transportation device to form a test system, and the test system is also provided with an intelligent control system, so that intelligent control and data monitoring of the system can be performed through the intelligent control system.\|[0037] The mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment.\|[0038] Specifically, the reaction main body is provided with a reaction tank 1 for mineralizing reaction materials; a mechanical stirring device 2 is arranged in the reaction tank 1, and the mineralization reaction can be promoted to be carried out through the mechanical stirring device 2; the upper end of the reaction tank 1 is connected with bubble generating equipment arranged at the outer end through a connecting pipeline, the bubble generating equipment comprises a carbon dioxide micro-bubble generator 3 and a gas cylinder 4, the gas cylinder 4 is connected to the carbon dioxide micro-bubble generator 3, and carbon dioxide is injected into the carbon dioxide micro-bubble generator 3 through the gas cylinder 4.\|[0039] Furthermore, the bubble generating equipment is also provided with a flowmeter 6 and a gas control valve 5, and the flowmeter 6 and the gas control valve 5 are arranged on a connecting pipeline connected with the outer end of the bubble generating equipment; the bubble generating device is used for improving the mineralization reaction efficiency by introducing carbon dioxide and water into the mineralization reaction device in a micro-nano bubble mode.\|[0040] As shown in fig. 1, the lower end of the reaction tank 1 is connected with an ultrasonic generating device through a connecting line, the ultrasonic generating device comprises an ultrasonic generating device 7 and an ultrasonic transducer 8, the ultrasonic transducer 8 is fixedly arranged at the bottom of the reaction tank 1, the ultrasonic generating device 7 is connected with the reaction tank 1 through the ultrasonic transducer 8, the power of ultrasonic waves can be controlled through the ultrasonic generating device 7, the mineralization effect can be improved, and the mineralization of carbon dioxide is promoted.\|[0041] Still further, the ultrasonic wave generating means 7 may be an ultrasonic wave generator or other ultrasonic wave generating device.\|[0042] Furthermore, a pressure sensor 9 and a temperature sensor 10 are also connected to the reaction tank 1 for monitoring the reaction pressure and the reaction temperature in the reaction tank 1.\|[0043] The reaction tank 1 is provided with a mineralization reaction material conveying port through which mineralization reaction materials can be added into the reaction tank 1; the bottom end of the reaction tank 1 is connected with a filling pump 11 and a paste filling pipeline 12, so that mineralized filling paste after being fully mixed is conveyed to a conveying device for conveying through the paste filling pipeline 12, and a conveying control valve 13 is arranged on the paste filling pipeline 12 and used for controlling the conveying of the mineralized filling paste.\|[0044] As shown in fig. 2, the transportation device comprises a plurality of sectional detachable connection type mineralized material transportation pipelines 14, an electromagnetic flowmeter 15 and a piezoresistive pressure sensor 16, wherein the electromagnetic flowmeter 15 is arranged at the inlet of the mineralized material transportation pipelines 14, and a mineralized material sampling port 17 is arranged at the outlet of the mineralized material transportation pipelines 14, so that sampling and monitoring are facilitated. The transportation device simulates the pipeline transportation of mineralized materials in a mineralized filling site, and the flow condition of the mineralized materials in the pipeline is monitored in real time through the electromagnetic flowmeter 15 and the piezoresistive pressure sensor 16.\|[0045] Further, a plurality of piezoresistive pressure sensors 16 are provided at a certain distance from each other inside the mineralized material transporting pipe 14 for pressure monitoring of the paste material transported in the pipe.\|[0046] As shown in fig. 3 and 4, the mineralization simulation device is an integrated treatment device for curing, molding and loading mineralization reaction materials, and comprises a curing part, a loading part and a molding part, wherein the curing part, the loading part and the molding part are all arranged in the device main body 18; the curing part is arranged in the loading part, and when the loading test is not performed, the curing part is used for performing natural curing of the mineralized material, and the loading part is used for performing a triaxial loading test of the mineralized material.\|[0047] Specifically, the curing part is a material placing area 19 arranged at the inner side of the loading part and used for placing mineralized materials for curing and loading test; the loading part is provided with a triaxial loading device 20, the compression strength of the sample after the mineralized material is loaded, analyzed and mineralized by the triaxial loading device 20, the triaxial loading device 20 comprises a triaxial loading original pressure head 21, a triaxial loading slotted pressure head 22, a loading baffle plate 23 and an electrical instrument 29, the triaxial loading slotted pressure head 22 is arranged at the inner end of the triaxial loading original pressure head 21 and is connected through threads, and the loading pressure head and the loading baffle plate 23 are arranged at the outer peripheral side of the material placing area 19.\|[0048] The shaping portion includes electric plate 24 and electric plate controller 25, and shaping portion sets up in the below of triaxial loading device 20, heats up mineralization analogue means through the electric plate 24 of shaping portion, detects temperature change through temperature sensor after the intensification, adjusts the scope of control mineralization analogue means inside temperature to the heating element, can also change the shaping ambient temperature of test block through electric plate 24 and simulate the temperature in goaf mineralization region moreover.\|[0049] Further, as a preferred embodiment of the present invention, the electric heating plate 24 is a constant temperature graphite electric heating plate.\|[0050] Further, as a preferred embodiment of the present invention, the loading plate 23 is disposed at the inner end of the triaxial loading slot die 22, the loading plate 23 has a square plate structure, and the triaxial loading slot die 22 can abut against the loading plate 23, so that a loading force can be applied to the sample placed in the material placement region 19; and the triaxial loading device 20 is provided with a plurality of groups of loading pressure heads and loading baffles 23 which are connected in a matched manner, so that triaxial loading tests can be carried out on the samples.\|[0051] Further, the loading baffle 23 is divided into an upper part and a lower part, the lower loading baffle is arranged on the base at the lower end, and the upper loading baffle and the lower loading baffle are connected with two ends of the notch of the triaxial loading slotting pressure head 22 through threads; the triaxial loading grooving head 22 is provided with a variety of grooving dimensions, the angle being variable, and the shape and size of the loading plate 23 being variable, so as to accommodate variations in the size and inclination of the mineralised reaction material.\|[0052] Specifically, as shown in fig. 4, the upper end of the device main body 18 is further provided with a sealing cover 26 for sealing the device, so as to ensure the air tightness of the device; the sealing cover 26 is provided with an air outlet 27 and a sensor interface 28, the air inside the device is sampled and detected through the air outlet 27, the bubble stability of the mineralized sample can be judged through detection, and the sensor interface 28 can be used for connecting a temperature sensor and a pressure sensor for temperature and pressure monitoring and controlling the loading process through an electromethod instrument 29.\|[0053] Furthermore, before closing the sealing cover 26, high vacuum silicone grease is applied to the contact surface between the sealing cover 26 and the loading part arranged at the lower side to ensure the air tightness of the device.\|[0054] Example 1\|[0055] The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|[0056] step 1: the mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline joint of the transportation device, so that a mineralization reaction system is formed.\|[0057] Step 2: the mineralized reaction material is weighed and prepared, and is filled into a mineralized reaction device.\|[0058] Specifically, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 The composition and the optimal proportion of each part of mineralization reaction material are shown in the following table.\|[0059] TABLE 1 mineralization reaction materials composition materials and proportion table thereof\|[0060] \|[0061] The CTABs listed in table 1 are cetyltrimethylammonium bromide.\|[0062] Specifically, the filling pump 11 and the delivery control valve 13 at the bottom end of the reaction tank 1 are closed, and the prepared mineralized reaction material is added into the reaction tank 1 through the mineralized reaction material delivery port.\|[0063] Step 3: opening a gas control valve 5 and a carbon dioxide micro-bubble generator 3 of the bubble generating equipment, firstly adding a certain amount of water into the carbon dioxide micro-bubble generator 3, then introducing carbon dioxide in a gas cylinder 4 into the carbon dioxide micro-bubble generator 3, generating an aqueous solution containing micro-nano carbon dioxide bubbles through the device, and then introducing the aqueous solution into a reaction tank 1 to start mineralization reaction; the mechanical stirring device 2 and the ultrasonic generating device 7 arranged in the reaction tank 1 are opened to improve the mineralization reaction efficiency of the reaction tank 1.\|[0064] After the mineralized reaction material and carbon dioxide in the reaction tank 1 fully react, a filling pump 11 and a conveying control valve 13 connected with the bottom end of the reaction tank 1 are opened, and the fully mixed mineralized reaction material is conveyed to a mineralization simulation device in a paste form through a paste filling pipeline 12 by a conveying device.\|[0065] Step 4: a piezoresistive pressure sensor 16, an electromagnetic flowmeter 15 and a mineralized material sampling port 17 in the transportation device are opened, and the transportation condition of mineralized filling paste in a transportation pipeline is observed; because the system is provided with the intelligent control system, the intelligent control system is utilized to collect data online, the pressure sensor, the temperature sensor and the electromagnetic flowmeter 15 in each experimental process collect data once every 60 seconds, and the filling paste at the output port of the conveying device is sampled and analyzed through the mineralized material sampling port every 5 minutes.\|[0066] Specifically, whether the filled paste can be transported smoothly in the pipeline without blocking the pipeline is judged by analyzing the data of the pressure sensor, the temperature sensor and the electromagnetic flowmeter, and whether the filled paste still can meet the paste pumping requirement after long-time pipeline transportation is judged by analyzing the paste slump and the paste layering change value of the sample of the mineralized material sampling port 17; the transportation condition of the filling paste in the pipeline is monitored in real time through the piezoresistive pressure sensor 16 and the sampling port to observe whether the mineralized filling paste can be transported smoothly.\|[0067] Step 5: opening a sealing cover 26 on the triaxial loading device 20, conveying the conveyed mineralized filling paste to a material placing area 19 in the mineralized simulation device through a conveying pipeline, and then closing the sealing cover 26 to ensure the air tightness in the device; the gas is sampled for the first time through the gas outlet 27 on the device main body 18, the sampled gas is subjected to component analysis through an experimental instrument, analysis data are recorded, and then the gas outlet 27 is closed to ensure the gas tightness of the device.\|[0068] The mineralized material is naturally cured for 12 hours, after 12 hours, the test block is completely solidified, and then a triaxial loading test can be carried out.\|[0069] Step 6: opening the sensor interface 28, and observing the change of the temperature and the pressure inside the device through the temperature and the pressure sensor; loading a mineralization reaction test block by simulating the stress condition of the goaf through a mineralization simulation device, and changing the temperature of the test block through an electric heating plate 24 of a forming part to simulate the temperature of a mineralization area of the goaf; the test block is subjected to a triaxial loading experiment according to the stress condition of the filled goaf by the triaxial loading device 20, and the forming environment temperature of the mineralized sample is changed by the electric heating plate 24.\|[0070] Step 7: when the sensor detects that the pressure in the device is kept unchanged for a long time, the mineralization reaction is finished, the air outlet 27 is opened to extract the air, the air in the device is collected for the second time, the analysis of the second air component is carried out, and the analysis result is compared with the analysis result of the first component;\|[0071] the existence condition of the internal bubbles of the coagulated test block after triaxial loading test with certain strength can be judged through comparison of the two groups of data, a part of bubbles are destroyed after triaxial loading, and the internal carbon dioxide gas is dispersed, so that the gas component of the loading device is changed, and the two gas analyses can be different.\|[0072] Step 8: finally, all the gases in the mineralization simulation device are extracted through the air outlet holes 27, and the gas component analysis is carried out to obtain the content change of carbon dioxide in the gases; according to the known total amount of the carbon dioxide gas cylinder, the content of carbon dioxide gas introduced into the system and the content of carbon dioxide which can be absorbed by the mineralization reaction material in theory, the content of carbon dioxide fixed by bubbles in the test block after the triaxial loading test can be obtained, and the mineralization effect of the mineralization material can be judged by the value.\|[0073] Therefore, the stability of the mineralized carbon dioxide can be verified, the efficiency of the mineralized reaction for absorbing the carbon dioxide can be calculated, and the compressive strength of the mineralized test block can be obtained through the damage condition of the test block after the triaxial loading test, so that whether the mineralized filling material can well fill the goaf can be judged.\|[0074] Example two\|[0075] The embodiment provides a method for dynamically simulating and mineralizing and sealing carbon dioxide in flue gas to fill a goaf, which comprises the following steps:\|[0076] step 1: the mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline joint of the transportation device, so that a mineralization reaction system is formed.\|[0077] Step 2: the mineralized reaction material is weighed and prepared, and is filled into a mineralized reaction device.\|[0078] Specifically, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 The composition and the optimal proportion of each part of mineralization reaction material are shown in the following table.\|[0079] TABLE 1 mineralization reaction materials composition materials and proportion table thereof\|[0080] \|[0081] The CTABs listed in table 1 are cetyltrimethylammonium bromide.\|[0082] Specifically, H 2 O 2 The CATB is a foam stabilizer.\|[0083] Specifically, the filling pump 11 and the delivery control valve 13 at the bottom end of the reaction tank 1 are closed, and the prepared mineralized reaction material is added into the reaction tank 1 through the mineralized reaction material delivery port.\|[0084] Step 3: using dried air and analytically pure CO 2 Proportioning of simulated flue gas, recording CO 2 The percentage of gas was set to a%.\|[0085] Since the composition of conventional fuel gas, fuel oil and coal flue gas is as follows: n (N) 2 :82%~89%,CO 2 :8%~15%,O 2 :3% -5%, a small amount of SO 2 Because of SO 2 The content of (C) is small, and the design is not considered, so that the dried air and pure CO for analysis are utilized 2 The composition of the flue gas can be simulated relatively accurately. (the normal air gas composition is as follows: N 2 :78%,O 2 21 percent of rare gas: 0.939%, CO 2 : 0.031), other gases and impurities: 0.03%).\|[0086] Step 4: opening a gas control valve 5 of a bubble generating device and a carbon dioxide micro-bubble generator 3, firstly adding a certain amount of water into the carbon dioxide micro-bubble generator 3, then introducing proportioned simulated flue gas, recording the total volume of the introduced gas as V, generating an aqueous solution containing micro-nano carbon dioxide bubbles through the device, and then introducing the aqueous solution into a reaction tank 1 to start mineralization reaction; the mechanical stirring device 2 and the ultrasonic generating device 7 arranged in the reaction tank 1 are opened to improve the mineralization reaction efficiency of the reaction tank 1.\|[0087] After the mineralized reaction material and carbon dioxide in the reaction tank 1 fully react, a filling pump 11 and a conveying control valve 13 connected with the bottom end of the reaction tank 1 are opened, and the fully mixed mineralized reaction material is conveyed to a mineralization simulation device in a paste form through a paste filling pipeline 12 by a conveying device.\|[0088] Step 5: a piezoresistive pressure sensor 16, an electromagnetic flowmeter 15 and a mineralized material sampling port 17 in the transportation device are opened, and the transportation condition of mineralized filling paste in a transportation pipeline is observed; because the system is provided with the intelligent control system, the intelligent control system is utilized to collect data online, the pressure sensor, the temperature sensor and the electromagnetic flowmeter 15 in each experimental process collect data once every 60 seconds, and the filling paste at the output port of the conveying device is sampled and analyzed through the mineralized material sampling port every 5 minutes.\|[0089] Specifically, whether the filled paste can be transported smoothly in the pipeline without blocking the pipeline is judged by analyzing the data of the pressure sensor, the temperature sensor and the electromagnetic flowmeter, and whether the filled paste still can meet the paste pumping requirement after long-time pipeline transportation is judged by analyzing the paste slump and the paste layering change value of the sample of the mineralized material sampling port 17; the transportation condition of the filling paste in the pipeline is monitored in real time through the piezoresistive pressure sensor 16 and the sampling port to observe whether the mineralized filling paste can be transported smoothly.\|[0090] Step 6: opening a sealing cover 26 on the triaxial loading device 20, conveying the conveyed mineralized filling paste to a material placing area 19 in the mineralized simulation device through a conveying pipeline, and then closing the sealing cover 26 to ensure the air tightness in the device; the gas is sampled for the first time through the gas outlet 27 on the device main body 18, the sampled gas is subjected to component analysis through an experimental instrument, analysis data are recorded, and then the gas outlet 27 is closed to ensure the gas tightness of the device.\|[0091] Specifically, the CO in the gas is obtained by sampling analysis 2 The proportion of the gas is b percent, and the gas which can chemically react with mineralized reaction materials in the simulated flue gas is mainly CO 2 The other reactive gases are of a smaller and negligible content and therefore can pass through the initial state CO 2 The ratio of the catalyst to the catalyst is a) and the residual CO in the mineralization reaction device after the reaction can be obtained 2 The content is as follows\|[0092] CO consumed by mineralization 2 The content is->\|[0093] And (3) carrying out natural maintenance on the mineralized material, and carrying out a triaxial loading test after the test block is completely solidified.\|[0094] Step 7: opening the sensor interface 28, and observing the change of the temperature and the pressure inside the device through the temperature and the pressure sensor; loading a mineralization reaction test block by simulating the stress condition of the goaf through a mineralization simulation device, and changing the temperature of the test block through an electric heating plate 24 of a forming part to simulate the temperature of a mineralization area of the goaf; the test block is subjected to a triaxial loading experiment according to the stress condition of the filled goaf by the triaxial loading device 20, and the forming environment temperature of the mineralized sample is changed by the electric heating plate 24.\|[0095] Step 8: when the pressure in the device is detected to be unchanged for a long time through the sensor, the mineralization reaction is considered to be finished, after the loading test is finished, the mineralization reaction test block is fully compressed until the gas fixed by bubbles in the test block is completely crushed and completely released, at the moment, the compression strength of the mineralization reaction test block can be obtained through the mineralization loading device, then the gas is extracted through the gas outlet 27, the gas in the device is collected for the second time, the analysis of the gas component for the second time is carried out, and the analysis result of the first component are calculated, so that the pressure-resistant strength of the mineralization reaction test block can be obtainedCO immobilized by bubbles on mineralized reaction test block 2 And (3) gas.\|[0096] The existence condition of the internal bubbles of the coagulated test block after triaxial loading test with certain strength can be judged through comparison of the two groups of data, a part of bubbles are destroyed after triaxial loading, and the internal carbon dioxide gas is dispersed, so that the gas component of the loading device is changed, and the two gas analyses can be different.\|[0097] Step 9: finally, all the gases in the mineralization simulation device are extracted through the air outlet holes 27, and the gas component analysis is carried out to obtain the content change of carbon dioxide in the gases; CO consumed by mineralization 2 Content, CO immobilized by bubbles in mineralized reaction block 2 The mineralization effect of the mineralization material is comprehensively judged by the content and the pressure bearing condition of the mineralization test block.\|[0098] Therefore, the stability of the mineralized carbon dioxide can be verified, the efficiency of the mineralized reaction for absorbing the carbon dioxide can be calculated, and the compressive strength of the mineralized test block can be obtained through the damage condition of the test block after the triaxial loading test, so that whether the mineralized filling material can well fill the goaf can be judged.\|[0099] Example III\|[0100] The embodiment provides a simulation experiment under different stress loading, and the manufacturing process and the proportion of the mineralization reaction test block of the embodiment are guaranteed to be the same as those of the embodiment one, and specifically comprises the following steps:\|[0101] step 1: weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|[0102] step 2: using dried air and analytically pure CO 2 Proportioning of simulated flue gas, recording CO 2 The percentage of the gas is set as a%;\|[0103] step 3: adding water into bubble generation equipment, then introducing proportioned simulated flue gas, recording the total volume of the introduced gas as V carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into a mineralization reaction device for mineralization reaction;\|[0104] step 4: conveying the fully mixed mineralized filling paste through a conveying device, collecting data of temperature and pressure in the system, sampling and analyzing the filling paste at an output port through a mineralized material sampling port 17, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through a pipeline monitoring device;\|[0105] step 5: the transported mineralized filling paste is transported to a mineralization simulation device through a transportation pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and the CO in the gas at the moment is obtained 2 The proportion of the gas is b percent, and the gas which can chemically react with mineralized reaction materials in the simulated flue gas is mainly CO 2 The other reactive gases are of a smaller and negligible content and therefore can pass through the initial state CO 2 The ratio of the catalyst to the catalyst is a) and the residual CO in the mineralization reaction device after the reaction can be obtained 2 The content is as follows:\|[0106] CO consumed by mineralization 2 The content is->\|[0107] And then naturally curing the mineralized material until the mineralized material is completely solidified.\|[0108] Step 6: the specific compressive strength of the test block can be known through the mineralization loading experiment of the first embodiment, the compressive strength is divided stepwise according to the compressive strength obtained in the first embodiment, the compressive strength is loaded step by step from low to high through the electrical instrument 29, and the damage degree of the test block during loading of each stage is obtained through analyzing the gas extracted from the gas outlet hole.\|[0109] Example IV\|[0110] The present example provides a secondary mineralization test under triaxial loading, and the mix ratio of mineralization reaction test blocks is the same as that of example one.\|[0111] In the solidification process of the mineralized reaction test block, simulating the stress condition of filling the goaf to carry out loading experiments on the test block, and introducing enough CO into the device in the loading process 2 Gas to mineralize reaction testThe block is subjected to secondary mineralization in loading, so that the mineralization sealing quantity is increased, the mineralization rate is improved, and the mineralization effect is enhanced.\|[0112] In mineralization reaction test block in CO 2 After the mineralization reaction is completed in the gas environment, the test block is subjected to a loading experiment again after the test block is completely solidified, the compression strength of the test block obtained by the loading experiment is compared with the compression strength of the test block obtained by the first experiment, and the degree of strengthening of the mineralization reaction by secondary mineralization is judged.\|[0113] The invention has simple and convenient simulation operation, is economical and feasible, and accords with the concept of green exploitation; by adding foaming agents such as hydrogen peroxide, aluminum powder, silica fume and the like into the mineralized reaction material, the void ratio of the mineralized material after complete reaction solidification is improved, and the filling volume is enlarged; the method comprises the steps of generating an aqueous solution containing micro-nano carbon dioxide bubbles by a micro-nano bubble generating device from carbon dioxide gas and water, introducing a mineralization reaction material to promote mineralization reaction, improving mineralization reaction rate, combining mechanical stirring and ultrasonic waves, and promoting mineralization reaction by using cavitation of ultrasonic waves and mechanical stirring.\|[0114] The transportation device adopts a sectional type transportation pipeline to simulate the transportation of mineralized filling paste on a filling site, the mineralization simulation device simulates the stress condition of a goaf to load a mineralization reaction test block, the heating device changes the temperature of the test block to simulate the temperature of a mineralization area of the goaf, and the triaxial loading device performs triaxial loading experiments on the test block in the mineralization simulation device according to the stress condition of the filling goaf, so that the test environment is ensured to be more attached to a real operation environment, and the simulation result is feasible and effective; by analyzing the gas after loading, the aim of detecting whether the mineralized filling paste can realize goaf filling is fulfilled.\|[0115] In the description of the present invention, it should be understood that the directions or positional relationships such as the terms "length", "width", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of description and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present application.\|[0116] Furthermore, in the description of the present application, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.\|[0117] The foregoing description of the preferred embodiments of the present application is not intended to be limiting, but is intended to cover any and all modifications, equivalents, and alternatives falling within the spirit and principles of the present application.	Family Number\|(105563865)\|105563865\|Advantages / Prev. Drawbacks\|(CN116359471 A)\|( . . . ) treatment are the key problems of attention in various fields , and the proposal of carbon dioxide mineralization sealing gives a solution thought , wherein the carbon dioxide mineralization sealing mainly imitates and accelerates the process of rock weathering and carbon dioxide absorption in nature , carbon dioxide is dissolved in water to generate carbonic acid , then the carbonic acid reacts with alkaline minerals to generate stable solid carbonate , and the stable solid carbonate can not be decomposed ( . . . ) \|Independent Claims\|(CN116359471 A)\|1. A system for dynamically simulating mineralization and sequestration of carbon dioxide filling goaf , comprising : the mineralization reaction device consists of a reaction main body , ultrasonic wave generating equipment and bubble generating equipment ; the conveying device is provided with a conveying pipeline and a pipeline ( . . . ) \|	Analysis of biological materials\|Civil engineering	E21F-015/00\|G01N-033/24		E21F-015/00\|G01N-033/24	E21F-015/00\|G01N-033/24	E21F-015/00\|G01N-033/24			CN117740754\|CN117491564\|CN117233253B\|CN116988839B	CN117740754 108978052 WHO=Examiner SELF=N CAT=A\|CN117491564 108407880 WHO=Examiner SELF=Y CAT=A\|CN117233253B 107757227 WHO=Examiner SELF=N\|CN116988839B 107136135 WHO=Examiner SELF=N	CN219910866U\|CN114673552\|US20230038447\|CN114179223\|KR20120076877	CN219910866U 107039211 WHO=Examiner SELF=Y CAT=L\|CN114673552 100630442 WHO=Examiner SELF=Y CAT=A\|US20230038447 103686458 WHO=Examiner SELF=N CAT=A\|CN114179223 99111724 WHO=Examiner SELF=N CAT=A\|KR20120076877 35305246 WHO=Examiner SELF=N CAT=A		KR20120076877; CN114179223; CN114673552; US20230038447; CN219910866U		PENDING	(CN116359471)\|PENDING	ALIVE	(CN116359471)\|ALIVE	(CN116359471)\|LEGAL DETAILS FOR CN116359471\|Actual or expected expiration date=2043-03-09\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-03-09\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202310241385\|Application date=2023-03-09\|Standardized application number=2023CN-0241385\|Event publication date=2023-06-30\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN116359471\|Publication stage code=A\|Publication date=2023-06-30\|Standardized publication number=CN116359471\|Event publication date=2023-06-30\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2023-07-18\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN116359471)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTq/xzSxeC8O1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000068491530&ekey=2040&xpn=CN116359471&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=6hhkKvFjdVxIIQir0tZck5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN116359471)\|CN	(CN116359471)\|NAME=ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN		(CN116359471)\|NAME=LONG JUNBO;WEIHAI HENG YU RUN DA PATENT AGENCY OFFICE (GENERAL PARTNERSHIP) , REG=37260		(CN116359471)\|NAME=WANG CHANGXIANG\|NAME=LU YAO\|NAME=ZHOU YONGQIANG\|NAME=LU WEI\|NAME=LI JINLIANG\|NAME=LI JINHU\|NAME=ZHUO HUI\|NAME=ZHANG QINGSONG\|NAME=ZHAO SHUJIE\|NAME=LI QINGHAI\|NAME=SI LEILEI\|NAME=JIANG NING	(CN116359471)\|4	1	1					(CN116359471)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2023-06-30\|Gazette number: GAZNUM=39-2602\|Number of Pages: NPAGES=14\|		(CN116359471)\|CHINESE (CHI)	(CN116359471)\|Patent	Titre: (CN116359471)\|System and method for dynamically simulating mineralized sealed carbon dioxide filled goaf Résumé: (CN116359471)\|The invention discloses a system and method for dynamically simulating mineralized sealed carbon dioxide filled goaf, and belongs to the technical field of mineralized sealed carbon dioxide. The device is provided with a mineralization reaction device, a transportation device and a mineralization simulation device, the mineralization reaction device is composed of a reaction main body, an ultrasonic generation device and a bubble generation device, the transportation device is provided with a transportation pipeline and a pipeline monitoring device, and the mineralization simulation device comprises a triaxial loading device and a heating device. The triaxial loading equipment is provided with a material supporting part and a loading assembly. The mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline connector of the transportation device, so that the mineralization reaction system is formed, then the mineralization sealed carbon dioxide filling goaf is dynamically simulated through the mineralization reaction system, and the method is simple and convenient in simulation operation, economical and feasible and conforms to the concept of green mining.	38	Abstract	gpt-4o-mini	no	The focus is on simulating mineralized sealed carbon dioxide in goaf, not on accelerating the weathering of minerals for CO₂ capture.
38	DE102024102958	WOEP2025/052349\|DE102024102958	WO2025/163040\|DE102024102958	115032330	WO2025/163040 A1 2025-08-07 [WO2025163040]\|DE102024102958 B3 2025-06-26 [DE102024102958]	2024-02-02	2025-01-30\|2024-02-02	2025-08-07\|2025-06-26	\|(DE102024102958)\|2025-06-26	(WO2025/163040)\|2027-08-02\|(DE102024102958)\|2044-02-02	(WO2025/163040)\|Method for the thermal treatment of raw meal using an electric heating device, and corresponding system	(WO2025/163040)\|The invention relates to a method for thermally treating raw meal in order to produce burnt lime and to a corresponding system. According to the invention, raw meal is thermally treated at an electrically heated heating contact. This leads to an exhaust gas which is free of nitrous gases and other organic constituents. The pure exhaust gas can be subjected to sequestration without any further special purification processes.	KHD HUMBOLDT WEDAG	(WO2025/163040)\|KHD HUMBOLDT WEDAG GMBH ([DE])\|(DE102024102958)\|KHD Humboldt Wedag GmbH ([DE])	FEISS MARC\|KNOCH ALEXANDER\|MERSMANN MATTHIAS	(WO2025/163040)\|FEISS, Marc\|KNOCH, Alexander\|MERSMANN, Matthias		(WO2025/163040)\|In order to seal off the reactor in which the screw conveyor is arranged from the atmosphere, it is advantageously provided that the raw meal is also fed to the reactor via a star feeder. The feeding and removal of the raw meal via a cellular wheel sluice in all reactor types mentioned here has the advantage that a relatively pure exhaust gas of carbon dioxide (CO2) is produced as the exhaust gas, which only contains water (H2O) as a further constituent.\|It would be desirable to carry out the process for the thermal treatment of lime in such a way that the expensive waste gas purification before the sequestration is not necessary.\|On the other hand, the distance must also not be so small that the raw meal 10 falls through a pipeline as if it were a pipe and rolls against the gas flowing up, so that the gas and the freely trickling raw meal 10 block the path alternately.\|Since this heat does not have a very high temperature, the heat obtained from the vapors is suitable for drying other materials. The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive.\|	(WO2025/163040)\|1. Process for the thermal treatment of raw meal for the production of burnt lime, characterized by- Heating the raw meal (10) on an electrically heated heating contact. \|	(WO2025/163040)\|The aim of the invention is therefore to provide a method for thermally treating lime, in which exhaust gas purification prior to sequestration of the carbon dioxide (CO2) can be dispensed with. The object according to the invention is achieved in that the raw meal is heated on an electrically heated heating contact.\|The invention relates to a method for the thermal treatment of raw meal for producing burnt lime and a corresponding installation.\|The invention relates to a method for thermally treating raw meal in order to produce burnt lime and to a corresponding system.\|	(WO2025/163040)\|RAW MEAL(100,55)\|BURNT LIME(100,13)\|RAW MEAL TREATMENT(100,12)\|ELECTRIC HEATING(100,10)\|BURNT LIME PRODUCTION(100,2)\|TREATING RAW MEAL(60,1)\|BURNING RAW MEAL(56,1)\|LIME MEAL(48,1)\|RAW MEAL REMOVAL(41,1)\|CELLULAR WHEEL SLUICE(39,10)\|STAR FEEDER(35,2)\|SEQUESTRATION(32,11)\|REACTOR(31,30)\|TUBULAR REACTOR(27,5)\|ORGANIC COMPONENT(27,1)\|PRODUCING BURNT LIME(27,1)\|UNDULATING GAP(26,1)\|LIME TREATMENT(24,3)\|ELECTRICALLY HEATED HEATING CONTACT(23,19)\|EXPENSIVE WASTE GAS PURIFICATION(23,1)\|DUST SEPARATOR(22,6)\|PIPELINE(22,1)\|WASTE GAS PURIFICATION(22,1)\|HEAT(20,20)\|NITROUS GAS(18,3)\|EXHAUST GAS PURIFICATION(18,2)\|GAS PATH(16,2)\|LIME CALCINATION(15,6)\|CO2(14,17)\|SCREW CONVEYER(14,6)\|CALCINED RAW MEAL(14,3)\|SILICATE(14,3)\|INCLINED ARRANGEMENT(14,1)\|EXHAUST GAS(13,19)\|CARBON DIOXIDE EXHAUST GAS(13,1)\|PURIFICATION(12,1)\|ROCK(11,3)\|CASCADE(11,2)\|LIME THERMOLYSIS(11,2)\|ANOTHERSLIDING SURFACE(11,1)\|CYCLONE SEPARATOR(10,8)\|HORIZONTAL ARRANGEMENT(10,2)\|CARBON DIOXIDE(9,17)\|HEAT CONTACT(9,5)\|TREATMENT FLOW(9,2)\|RAW MEAL TURBULENCE(9,1)\|ABRASIVE RAW MEAL(8,1)\|BURNT RAW MEAL(8,1)\|VAPOR CELLULAR WHEEL SLUICE(8,1)\|BURNT PRODUCT(7,3)\|GAS COUNTERCURRENT(7,3)\|HEAT EXCHANGER(7,3)\|RAW FLOUR(7,2)\|SUSPENDED RAW MEAL(7,1)\|CLOUD SYMBOL(6,1)\|COUNTERCURRENT REACTOR(6,1)\|GRIND LIME(6,1)\|INSTALLATION REFINEMENT(6,1)\|RAW MEAL FLOWING(6,1)\|RAW MEAL HEATING(6,1)\|RAW MEAL SLIDE(6,1)\|CALCINATION PRODUCT(5,3)\|BURNED LIME(5,1)\|ENTRAIN BED REACTOR(5,1)\|FLAME PROJECT(5,1)\|PERMANENT DEPOSIT(5,1)\|SLIDE OVER(5,1)\|SLIDING OVER(5,1)\|FOOT(4,4)\|ROTARY VALVE(4,3)\|ELECTRICAL HEATING HEAT(4,2)\|DOWNSTREAM ROTARY KILN(4,1)\|GROUND LIME(4,1)\|INORGANIC BINDER(4,1)\|NATURAL DEPOSIT(4,1)\|NATURAL LIME(4,1)\|REACTOR 105(3,4)\|REGULATING FLOW(3,3)\|APPENDIX(3,1)\|AQUIFER(3,1)\|CAVERN(3,1)\|CELLULAR WHEEL LOCK(3,1)\|CEMENT CLINKER(3,1)\|\|(DE102024102958)\|RAW MEAL(100,35)\|REACTOR(100,19)\|HEAT(100,16)\|BURNT LIME(100,12)\|ELECTRICALLY HEATED HEATING CONTACT(100,11)\|RAW MEAL TREATMENT(100,8)\|ELECTRIC HEATING(100,6)\|BURNT LIME PRODUCTION(100,3)\|HEAT CONTACT(100,3)\|PLANT(100,3)\|SLIDE OVER(100,2)\|RAW MEAL FLOUR(77,1)\|BURNING RAW MEAL(57,1)\|LIME MEAL(49,1)\|RAW FLOUR(40,2)\|PRODUCING BURNT LIME(36,1)\|SEQUESTRATION(30,6)\|UNDULATING GAP(27,1)\|CASCADE(26,3)\|SLIDING SURFACE(25,24)\|EXPENSIVE WASTE GAS PURIFICATION(24,1)\|DUST SEPARATOR(23,3)\|EXHAUST GAS PURIFICATION(23,1)\|PIPELINE(23,1)\|WASTE GAS PURIFICATION(23,1)\|OFFSET ARRANGEMENT(22,1)\|TREATMENT FLOW(20,3)\|CELLULAR WHEEL SLUICE(15,4)\|LIME CALCINATION(14,5)\|SILICATE(14,3)\|ROCK(12,3)\|LIME THERMOLYSIS(11,2)\|SLIDING OVER(11,2)\|GAS PATH(11,1)\|CO2(10,4)\|HEAT EXCHANGER(10,3)\|ELECTRICALLY HEATED SLIDING SURFACE(9,4)\|HEATING213ROTARY LOCK214FLOW(9,1)\|RAW MEAL TRICKLING(9,1)\|GAS COUNTERCURRENT(7,3)\|CALCINED12RAW MEAL(7,1)\|INTERNET PUBLICATION HTTP(7,1)\|SUSPENDED RAW MEAL(7,1)\|UNBURNT11RAW MEAL(7,1)\|CARBON DIOXIDE(6,10)\|BURNING LIMESTONE(6,1)\|COUNTERCURRENT REACTOR(6,1)\|GRIND LIME(6,1)\|INSTALLATION REFINEMENT(6,1)\|RAW MEAL HEATING(6,1)\|RAW MEAL SLIDE(6,1)\|BURNT PRODUCT(5,2)\|NITROUS GAS(5,2)\|BURNED LIME(5,1)\|ENTRAIN BED REACTOR(5,1)\|FLAME PROJECT(5,1)\|CALCINATION PRODUCT(4,2)\|COMPRESSOR(4,2)\|CYCLONE SEPARATOR(4,2)\|ELECTRICAL HEATING HEAT(4,2)\|DOWNSTREAM ROTARY KILN(4,1)\|GROUND LIME(4,1)\|HEATING313ROTARY(4,1)\|INORGANIC BINDER(4,1)\|NATURAL DEPOSIT(4,1)\|NATURAL LIME(4,1)\|ROOF AREA(3,3)\|ARCHIVE(3,1)\|CEMENT CLINKER(3,1)\|CLIMATE(3,1)\|ELECTRICAL FIRE(3,1)\|	(WO2025/163040)\|P A T E N T A N S P R U C H E \|1. Process for the thermal treatment of raw meal for the production of burnt lime, characterized by\|- Heating the raw meal (10) on an electrically heated heating contact. \|2. Plant (100, 200, 300, 400) for carrying out the process according to Claim 1, having a reactor (105, 205, 305, 405) within which the electrically heated heating contact is arranged, which is designed such that the raw meal (10) slides over the electrically heated heating contact.\|3. An installation according to claim 2, characterized in that the electrically heated heating contact consists of a plurality of electrically heated heating contacts arranged vertically one above the other and offset in pairs relative to one another\|Sliding surfaces (110) exist, so that the raw meal (10) slides from top to top, as if via cascades, between the sliding surfaces (110) arranged in pairs, the sliding surfaces (110) being arranged in the reactor (105). \|4. Plant according to Claim 3, characterized in that the sliding surfaces (210) have openings through which gas produced during the thermal treatment flows and additionally heats the raw meal (10) sliding over the sliding surfaces (210).\|5. An installation according to claim 4, characterized in that the electrically heated heating contact consists of a plurality of vertically arranged and wave-shaped sliding surfaces (310) which are arranged parallel to one another and form an undulating gap in pairs between them.\|6. Plant according to claim 2, characterized in that the reactor (405) is tubular and the electrically heated heating contact is embedded in the bottom of the tubular reactor (405), the tubular reactor (405) having a horizontal or inclined arrangement, within which a screw conveyor (450) is arranged which moves the raw meal (10) over the electrically heated heating contact.\|7. Plant according to one of Claims 2 to 6, characterized in that the reactor (105, 205, 305, 405) has at least one discharge opening for the vapors produced during the thermal treatment, which discharge opening is connected to a dust separator (212, 312, 412) which separates raw meal (10) from the vapors.\|8. Plant according to Claim 7, characterized in that a heat exchanger (102) is arranged in the gas path and dissipates heat from the vapors (115) emerging from the gas paths.	(WO2025/163040)\|[0001] Process for the thermal treatment of raw meal using an electric heating device and corresponding installation \| [0002] The invention relates to a method for the thermal treatment of raw meal for producing burnt lime and a corresponding installation.\| [0003] For the production of burnt lime (CaO), it is known to grind lime (CaCOs) from natural deposits finely into so-called raw meal and to dry it suspended in a gas stream and to supply it to a thermal treatment. Burned lime (CaO) is, in addition to other substances, a starting material for the production of cement clinker, but also for the production of soda. Lime burnt is also used as a base in various chemical processes and is used in inorganic binders. Ground calcined lime is named differently depending on the industry. In the cement industry, a flour of a mixture of burnt lime and silicate-containing rock is called "raw flour". In other sectors, the pure burnt lime is also referred to as 'raw meal'. For the firing, i.e. thermal treatment of lime (CaCOs) in the form of raw meal, as a rule a flue-flow reactor is used into which a flame projects or, depending on the further process control, hot exhaust gases from a downstream rotary kiln are passed. In this thermal treatment, not only is carbon dioxide (CO2) formally driven out of the natural lime (CaCOs), which is an endothermic process, but because of the high activation energy, a comparatively high temperature of about 800°C is necessary in order to initiate the thermolysis of the lime (CaCOs). In order to generate the high temperature, it is necessary to burn fuel, the flame passing into the entrained-bed reactor. The exhaust gases from the calcination process that takes place contain carbon dioxide (CO2) from the burnt lime (CaCOs) and also carbon dioxide (CO2) from the combustion of fossil fuels. In addition to carbon dioxide (CO2), the exhaust gas also contains nitrous gases (NOx) and other exhaust gas constituents, such as volatile organic compounds (VOCs). In order to sequester the carbon dioxide (CO2) from the exhaust gas, which is recognized as harmful to the climate, it is necessary to subject the exhaust gas to a purification in order to separate air nitrogen (N2), the nitrous gases and the VOC from the exhaust gas before sequestration. \| [0004] It would be desirable to carry out the process for the thermal treatment of lime in such a way that the expensive waste gas purification before the sequestration is not necessary. \| [0005] The aim of the invention is therefore to provide a method for thermally treating lime, in which exhaust gas purification prior to sequestration of the carbon dioxide (CO2) can be dispensed with. \| [0006] The object according to the invention is achieved in that the raw meal is heated on an electrically heated heating contact. The installation corresponding thereto has a reactor within which the electrically heated heating contact is arranged, which is designed such that the raw meal slides over the electrically heated heating contact. Further advantageous embodiments of the installation are specified in the subclaims to claim 2. \| [0007] According to the idea of the invention, it is therefore provided that the raw meal, irrespective of whether it is mixed with silicate-containing rock, as is customary in the cement industry, or whether the raw meal is present as pure ground lime, is heated on an electrically heated heating contact. In order to transfer the necessary amount of heat to the raw meal, it may be advantageous in a refinement of the installation according to the invention that the speed at which the raw meal is guided past the electrically heated heating contact is slowed down by a structural arrangement of sliding surfaces as electrically heated heating contact. For this purpose, in a first embodiment of the installation according to the invention, it can be provided that the electrically heated heating contact consists of a plurality of electrically heated sliding surfaces which are arranged vertically one above the other and offset in pairs relative to one another, so that the raw meal slides from top to bottom, as via cascades, between the sliding surfaces arranged in pairs, the sliding surfaces being arranged in the reactor. The plurality of electrically heated sliding surfaces, which are arranged in pairs offset with respect to one another and vertically one above the other, behave like baffles which slow down the flow of raw meal when the raw meal trickles over the sliding surfaces from top to bottom. \| [0008] In a further embodiment of the installation according to the invention, it can be provided that the sliding surfaces have openings through which gas produced during the thermal treatment flows and additionally heats the raw meal sliding over the sliding surfaces. The openings are open to the side and in the direction of the sliding raw meal, so that the raw meal does not fall through the openings. However, the gas, which comes from below, flows through the openings and thus also flows through the sliding raw meal. During this mixing, heat which is present in the gas is transferred to the raw meal, so that it is additionally heated. The flow of the hot exhaust gases of the thermal treatment at lower stages of the electrically heated heating contact thus means a recuperation of the heat electrically introduced into the raw meal. \| [0009] In a further embodiment of the installation according to the invention, it can be provided that the electrically heated heating contact consists of a plurality of vertically arranged and wave-shaped sliding surfaces which are arranged parallel to one another. The wave-shaped sliding surfaces have a similar effect to the aforementioned sliding surfaces arranged in pairs offset relative to one another. However, the undulating sliding surfaces are arranged so close to one another that a mixture of trickling of the raw meal and turbulence of the raw meal due to gas flowing up from below, which is produced during the thermal treatment, is established in the path forming between two undulating sliding surfaces and snaking in the vertical direction. \| [0010] In yet a further embodiment of the plant according to the invention, it can be provided that the reactor is tubular and the electrically heated heating contact is embedded in the bottom of the tubular reactor, the tubular reactor having a horizontal or oblique arrangement, within which a screw conveyor is arranged. The screw conveyor moves the raw meal over the electrically heated heating contact until the burnt raw meal is ejected at the end of the reactor via a cellular wheel sluice. In order to seal off the reactor in which the screw conveyor is arranged from the atmosphere, it is advantageously provided that the raw meal is also fed to the reactor via a star feeder. The feeding and removal of the raw meal via a cellular wheel sluice in all reactor types mentioned here has the advantage that a relatively pure exhaust gas of carbon dioxide (CO2) is produced as the exhaust gas, which only contains water (H2O) as a further constituent. Since the water can easily be condensed out, the waste gas obtained in this way is suitable for sequestration, for example by storage in aquifers or in caverns as permanent deposits. \| [0011] All reactor types presented here have a vapor outlet. However, the vapors, which consist essentially of carbon dioxide (CO2) and water (H2O), still contain suspended raw meal. The suspended raw meal can be separated in a cyclone separator. The exhaust gas emerging from the cyclone separator can furthermore be passed through a heat exchanger in order to remove the heat from the vapors as process heat. Since this heat does not have a very high temperature, the heat obtained from the vapors is suitable for drying other materials. \| [0012] The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive. If, however, electrical energy can be obtained from process heat elsewhere or from renewable energies, then electrical firing in conjunction with a necessary sequestration of the carbon dioxide (CO2) produced during firing is a variant which is also entirely attractive from an economic point of view and from a climate-related point of view. \| [0013] The invention is explained in more detail with reference to the following figures. It shows: \| [0014] FIG. 1 shows an installation for the thermal treatment of raw meal using an electric heating device in a first embodiment, \| [0015] FIG. 2 shows an installation for the thermal treatment of raw meal using an electric heating device in a second embodiment, \| [0016] FIG. 3 shows an installation for the thermal treatment of raw meal using an electric heating device in a third embodiment, \| [0017] FIG. 4 shows a plant for the thermal treatment of raw meal using an electric heating device in a fourth embodiment. \| [0018] FIG. 1 shows a first embodiment of an installation 100 for the thermal treatment of raw meal 10 using an electric heating device. Raw meal 10 is passed via a cellular wheel sluice 101 into a reactor 105, where the raw meal 10 trickles over a plurality of electrically heated sliding surfaces 110 which are arranged vertically one above the other and offset with respect to one another in pairs. The sliding surfaces 110 are provided on the rear side, that is to say on the underside, with an electrical resistance heater 111 which heats the sliding surfaces 110. The sliding surfaces 110 serve to protect the resistance heater 111 present thereunder, so that the abrasive raw meal does not close the resistance heaters 111. In this embodiment, the reactor 105 is designed to be gas-tight. Vapors 115 and carbon dioxide (CO2), both of which are formed during the electric burning of the lime (CaCOs), leave the reactor 105 together with the burnt or calcined raw meal 11 at the lower foot 106 of the reactor 105 and are passed into a cyclone separator 107. In the cyclone separator 107, the burnt or calcined raw meal 11 is separated from the vapors and the carbon dioxide (CO2). The finished product, i.e. the fired or calcined raw meal 11, leaves the cyclone separator 107 at its lower coarse material outlet 108. The gas, i.e. the vapors and the carbon dioxide (CO2) leave the cyclone separator 107 at its upper fines/gas outlet 109. The gas discharged there is purified again by a dust separator 112, still fine, burnt raw meal 12 being separated off. The purified exhaust gas, the vapors 115 and the carbon dioxide (CO2) are then discarded via a flow regulator 114 and a compressor 116 for extraction for sequestration. The cloud symbol shown here for the vapors 115 is not intended to mean that the exhaust gas is discarded into the atmosphere, but rather the exhaust gas is to be subjected to sequestration, not shown in detail here. The fractions of the finished product, namely the burnt or calcined lime 11, 12, are combined and fed to further use. \| [0019] FIG. 2 shows a second embodiment of an installation 200 for the thermal treatment of raw meal 10 using an electric heating device. The installation 200 differs from the embodiment shown in FIG. 1 in that the sliding surfaces 210 have openings through which vapors 215 and carbon dioxide (CO2), both of which are produced on the lower sliding surfaces 210, can flow through the respective upper sliding surfaces 210. In this case, the exhaust gas, namely the hot vapors 215 and the hot carbon dioxide (CO2), flows through the raw meal 10 on the respective upper sliding surfaces 210, as a result of which the raw meal flowing there is additionally heated. This additional heating of the raw meal 10 means a recuperation of the waste heat which is produced at the temperature necessary for the thermolysis of the lime (CaCO3) to burnt lime (CaO). In order that the raw meal does not fall through the openings, the openings are provided with a partial compartment surface D in the sliding direction. This partial roof area D is shown more clearly in the enlarged representation of the detail A. The partial roof area D is shown in FIGS. Unlike the reactor 105 in the embodiment in FIG. 1, the reactor 205 shown here is provided with a gas opening at the head 204 of the reactor 205 with a gas outlet. This arrangement of a gas outlet leads to a gas countercurrent within the reactor 205, which is represented by vertical arrows drawn in the reactor 205. The gas flows upwards into the gas discharge in the head 204 of the reactor 205, whereas the completely burnt or calcined product falls into the foot 206 of the reactor 205. There the completely burnt or calcined lime is discharged through a cellular wheel sluice 213. The burnt or calcined lime 11 separated in the dust separator 207 is combined with the product originating from the cellular wheel sluice 213. The exhaust gas, on the other hand, flows via a flow regulator 214 and compressor 216 to its further sequestration. \| [0020] FIG. 3 shows an installation 300 for the thermal treatment of raw meal 10 using an electric heating device in a third embodiment. In contrast to the cascade-like sliding surfaces 110 and 210 in the two embodiments mentioned above, it is provided in this embodiment that the sliding surfaces 310 are sliding surfaces 310 which are in the form of electrically heated heating contacts, are close to one another and have a wavy construction and between them form a sinuous or undulating gap extending essentially from top to bottom. Within the gap between two sliding surfaces 310, a mixing movement is formed from a trickling of the raw meal 10 and a gas countercurrent, in which the raw meal 10, which is present with the already partially burnt or calcined lime 11, is swirled up in a manner similar to that in a countercurrent reactor. The gas countercurrent has a heat-recuperating effect which has already been discussed with respect to the embodiment of the plant in FIG. 2. It is important here that the distance between the second sliding surfaces 310 is not too wide, so that a separation between the trickling of the raw meal and the upward flow of the exhaust gas cannot occur. On the other hand, the distance must also not be so small that the raw meal 10 falls through a pipeline as if it were a pipe and rolls against the gas flowing up, so that the gas and the freely trickling raw meal 10 block the path alternately. The sliding surfaces 310 are connected on one side to resistance heaters 311. The gas flows upwards into the gas discharge in the head 304 of the reactor 305, whereas the completely burnt or calcined product falls into the foot 306 of the reactor 305. There the completely burnt or calcined lime is discharged through a cellular wheel sluice 313. The burnt or calcined lime 11 separated in the dust separator 307 is combined with the product originating from the cellular wheel sluice 313. The exhaust gas, on the other hand, flows via a flow regulator 314 and compressor 2316 to its further sequestration. \| [0021] Finally, FIG. 4 shows an installation 400 for the thermal treatment of raw meal 10 using an electric heating device 410 in a fourth embodiment. A screw conveyor 450 is arranged in the reactor 405, which is shown as a tubular reactor 405 horizontally or obliquely ("obliquely" not shown here). This screw conveyor 450 transports the raw meal 10 introduced into the reactor 405 via a cellular wheel sluice 401 via the sliding surfaces 410 which are let into the lower wall 451 and are electrically heated from below by resistance heaters 411. This embodiment has the advantage that the dwell time of the raw meal 10 on the sliding surfaces 410 can be set as an electrically heated heating contact with the speed of the screw conveyor 450. Vapors 415 and carbon dioxide (CO2) are also produced as waste gas in this reactor 405. This exhaust gas is passed via gas discharge lines 460 to a dust separator 412 which separates raw meal 11 still suspended in the exhaust gas from the exhaust gas. The remaining exhaust gas from vapors 415 and carbon dioxide (CO2) is then subjected to sequestration. On the other hand, the completely burnt or calcined product from the cellular wheel sluice is combined with the separated product from the dust separator 412.\| [0022] B E Z U G S Z E I C H E N L I S E \| [0023] Raw meal, unburnt 200 plant\| [0024] Raw flour, calcined 201 star feeder\| [0025] Raw meal, calcined 204 head (reactor) \| [0026] 205 Reactor\| [0027] Appendix 206 feet (reactor)\| [0028] Rotary valve 207 cyclone separator\| [0029] Heat exchanger 208 coarse material discharge\| [0030] Reactor 209 fines/gas outlet\| [0031] Foot (reactor) 210 sliding surface\| [0032] Cyclone separator 211 resistance heating\| [0033] Coarse material outlet 213 rotary valve\| [0034] Fine/gas outlet 214 flow controller\| [0035] Sliding surface 215 vapors\| [0036] Resistance heating 216 Compressor\| [0037] dust collector \| [0038] Cellular wheel lock 300 system\| [0039] Flow controller 301 rotary valve\| [0040] Vapors 304 head (reactor)\| [0041] Compressor 305 reactor \| [0042] 306 feet (reactor) sliding surface 414 flow regulator resistance heater 415 vapors cellular wheel sluice 416 compressor flow regulator 450 screw conveyor vapors 451 wall compressor 460 gas discharge system A detail cellular wheel sluice D partial roof surface dust separator	(WO2025/163040)\|[0001] Process for the thermal treatment of raw meal using an electric heating device and corresponding installation \| [0002] The invention relates to a method for the thermal treatment of raw meal for producing burnt lime and a corresponding installation.\| [0003] For the production of burnt lime (CaO), it is known to grind lime (CaCOs) from natural deposits finely into so-called raw meal and to dry it suspended in a gas stream and to supply it to a thermal treatment. Burned lime (CaO) is, in addition to other substances, a starting material for the production of cement clinker, but also for the production of soda. Lime burnt is also used as a base in various chemical processes and is used in inorganic binders. Ground calcined lime is named differently depending on the industry. In the cement industry, a flour of a mixture of burnt lime and silicate-containing rock is called "raw flour". In other sectors, the pure burnt lime is also referred to as 'raw meal'. For the firing, i.e. thermal treatment of lime (CaCOs) in the form of raw meal, as a rule a flue-flow reactor is used into which a flame projects or, depending on the further process control, hot exhaust gases from a downstream rotary kiln are passed. In this thermal treatment, not only is carbon dioxide (CO2) formally driven out of the natural lime (CaCOs), which is an endothermic process, but because of the high activation energy, a comparatively high temperature of about 800°C is necessary in order to initiate the thermolysis of the lime (CaCOs). In order to generate the high temperature, it is necessary to burn fuel, the flame passing into the entrained-bed reactor. The exhaust gases from the calcination process that takes place contain carbon dioxide (CO2) from the burnt lime (CaCOs) and also carbon dioxide (CO2) from the combustion of fossil fuels. In addition to carbon dioxide (CO2), the exhaust gas also contains nitrous gases (NOx) and other exhaust gas constituents, such as volatile organic compounds (VOCs). In order to sequester the carbon dioxide (CO2) from the exhaust gas, which is recognized as harmful to the climate, it is necessary to subject the exhaust gas to a purification in order to separate air nitrogen (N2), the nitrous gases and the VOC from the exhaust gas before sequestration. \| [0004] It would be desirable to carry out the process for the thermal treatment of lime in such a way that the expensive waste gas purification before the sequestration is not necessary. \| [0005] The aim of the invention is therefore to provide a method for thermally treating lime, in which exhaust gas purification prior to sequestration of the carbon dioxide (CO2) can be dispensed with. \| [0006] The object according to the invention is achieved in that the raw meal is heated on an electrically heated heating contact. The installation corresponding thereto has a reactor within which the electrically heated heating contact is arranged, which is designed such that the raw meal slides over the electrically heated heating contact. Further advantageous embodiments of the installation are specified in the subclaims to claim 2. \| [0007] According to the idea of the invention, it is therefore provided that the raw meal, irrespective of whether it is mixed with silicate-containing rock, as is customary in the cement industry, or whether the raw meal is present as pure ground lime, is heated on an electrically heated heating contact. In order to transfer the necessary amount of heat to the raw meal, it may be advantageous in a refinement of the installation according to the invention that the speed at which the raw meal is guided past the electrically heated heating contact is slowed down by a structural arrangement of sliding surfaces as electrically heated heating contact. For this purpose, in a first embodiment of the installation according to the invention, it can be provided that the electrically heated heating contact consists of a plurality of electrically heated sliding surfaces which are arranged vertically one above the other and offset in pairs relative to one another, so that the raw meal slides from top to bottom, as via cascades, between the sliding surfaces arranged in pairs, the sliding surfaces being arranged in the reactor. The plurality of electrically heated sliding surfaces, which are arranged in pairs offset with respect to one another and vertically one above the other, behave like baffles which slow down the flow of raw meal when the raw meal trickles over the sliding surfaces from top to bottom. \| [0008] In a further embodiment of the installation according to the invention, it can be provided that the sliding surfaces have openings through which gas produced during the thermal treatment flows and additionally heats the raw meal sliding over the sliding surfaces. The openings are open to the side and in the direction of the sliding raw meal, so that the raw meal does not fall through the openings. However, the gas, which comes from below, flows through the openings and thus also flows through the sliding raw meal. During this mixing, heat which is present in the gas is transferred to the raw meal, so that it is additionally heated. The flow of the hot exhaust gases of the thermal treatment at lower stages of the electrically heated heating contact thus means a recuperation of the heat electrically introduced into the raw meal. \| [0009] In a further embodiment of the installation according to the invention, it can be provided that the electrically heated heating contact consists of a plurality of vertically arranged and wave-shaped sliding surfaces which are arranged parallel to one another. The wave-shaped sliding surfaces have a similar effect to the aforementioned sliding surfaces arranged in pairs offset relative to one another. However, the undulating sliding surfaces are arranged so close to one another that a mixture of trickling of the raw meal and turbulence of the raw meal due to gas flowing up from below, which is produced during the thermal treatment, is established in the path forming between two undulating sliding surfaces and snaking in the vertical direction. \| [0010] In yet a further embodiment of the plant according to the invention, it can be provided that the reactor is tubular and the electrically heated heating contact is embedded in the bottom of the tubular reactor, the tubular reactor having a horizontal or oblique arrangement, within which a screw conveyor is arranged. The screw conveyor moves the raw meal over the electrically heated heating contact until the burnt raw meal is ejected at the end of the reactor via a cellular wheel sluice. In order to seal off the reactor in which the screw conveyor is arranged from the atmosphere, it is advantageously provided that the raw meal is also fed to the reactor via a star feeder. The feeding and removal of the raw meal via a cellular wheel sluice in all reactor types mentioned here has the advantage that a relatively pure exhaust gas of carbon dioxide (CO2) is produced as the exhaust gas, which only contains water (H2O) as a further constituent. Since the water can easily be condensed out, the waste gas obtained in this way is suitable for sequestration, for example by storage in aquifers or in caverns as permanent deposits. \| [0011] All reactor types presented here have a vapor outlet. However, the vapors, which consist essentially of carbon dioxide (CO2) and water (H2O), still contain suspended raw meal. The suspended raw meal can be separated in a cyclone separator. The exhaust gas emerging from the cyclone separator can furthermore be passed through a heat exchanger in order to remove the heat from the vapors as process heat. Since this heat does not have a very high temperature, the heat obtained from the vapors is suitable for drying other materials. \| [0012] The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive. If, however, electrical energy can be obtained from process heat elsewhere or from renewable energies, then electrical firing in conjunction with a necessary sequestration of the carbon dioxide (CO2) produced during firing is a variant which is also entirely attractive from an economic point of view and from a climate-related point of view. \| [0013] The invention is explained in more detail with reference to the following figures. It shows: \| [0014] FIG. 1 shows an installation for the thermal treatment of raw meal using an electric heating device in a first embodiment, \| [0015] FIG. 2 shows an installation for the thermal treatment of raw meal using an electric heating device in a second embodiment, \| [0016] FIG. 3 shows an installation for the thermal treatment of raw meal using an electric heating device in a third embodiment, \| [0017] FIG. 4 shows a plant for the thermal treatment of raw meal using an electric heating device in a fourth embodiment. \| [0018] FIG. 1 shows a first embodiment of an installation 100 for the thermal treatment of raw meal 10 using an electric heating device. Raw meal 10 is passed via a cellular wheel sluice 101 into a reactor 105, where the raw meal 10 trickles over a plurality of electrically heated sliding surfaces 110 which are arranged vertically one above the other and offset with respect to one another in pairs. The sliding surfaces 110 are provided on the rear side, that is to say on the underside, with an electrical resistance heater 111 which heats the sliding surfaces 110. The sliding surfaces 110 serve to protect the resistance heater 111 present thereunder, so that the abrasive raw meal does not close the resistance heaters 111. In this embodiment, the reactor 105 is designed to be gas-tight. Vapors 115 and carbon dioxide (CO2), both of which are formed during the electric burning of the lime (CaCOs), leave the reactor 105 together with the burnt or calcined raw meal 11 at the lower foot 106 of the reactor 105 and are passed into a cyclone separator 107. In the cyclone separator 107, the burnt or calcined raw meal 11 is separated from the vapors and the carbon dioxide (CO2). The finished product, i.e. the fired or calcined raw meal 11, leaves the cyclone separator 107 at its lower coarse material outlet 108. The gas, i.e. the vapors and the carbon dioxide (CO2) leave the cyclone separator 107 at its upper fines/gas outlet 109. The gas discharged there is purified again by a dust separator 112, still fine, burnt raw meal 12 being separated off. The purified exhaust gas, the vapors 115 and the carbon dioxide (CO2) are then discarded via a flow regulator 114 and a compressor 116 for extraction for sequestration. The cloud symbol shown here for the vapors 115 is not intended to mean that the exhaust gas is discarded into the atmosphere, but rather the exhaust gas is to be subjected to sequestration, not shown in detail here. The fractions of the finished product, namely the burnt or calcined lime 11, 12, are combined and fed to further use. \| [0019] FIG. 2 shows a second embodiment of an installation 200 for the thermal treatment of raw meal 10 using an electric heating device. The installation 200 differs from the embodiment shown in FIG. 1 in that the sliding surfaces 210 have openings through which vapors 215 and carbon dioxide (CO2), both of which are produced on the lower sliding surfaces 210, can flow through the respective upper sliding surfaces 210. In this case, the exhaust gas, namely the hot vapors 215 and the hot carbon dioxide (CO2), flows through the raw meal 10 on the respective upper sliding surfaces 210, as a result of which the raw meal flowing there is additionally heated. This additional heating of the raw meal 10 means a recuperation of the waste heat which is produced at the temperature necessary for the thermolysis of the lime (CaCO3) to burnt lime (CaO). In order that the raw meal does not fall through the openings, the openings are provided with a partial compartment surface D in the sliding direction. This partial roof area D is shown more clearly in the enlarged representation of the detail A. The partial roof area D is shown in FIGS. Unlike the reactor 105 in the embodiment in FIG. 1, the reactor 205 shown here is provided with a gas opening at the head 204 of the reactor 205 with a gas outlet. This arrangement of a gas outlet leads to a gas countercurrent within the reactor 205, which is represented by vertical arrows drawn in the reactor 205. The gas flows upwards into the gas discharge in the head 204 of the reactor 205, whereas the completely burnt or calcined product falls into the foot 206 of the reactor 205. There the completely burnt or calcined lime is discharged through a cellular wheel sluice 213. The burnt or calcined lime 11 separated in the dust separator 207 is combined with the product originating from the cellular wheel sluice 213. The exhaust gas, on the other hand, flows via a flow regulator 214 and compressor 216 to its further sequestration. \| [0020] FIG. 3 shows an installation 300 for the thermal treatment of raw meal 10 using an electric heating device in a third embodiment. In contrast to the cascade-like sliding surfaces 110 and 210 in the two embodiments mentioned above, it is provided in this embodiment that the sliding surfaces 310 are sliding surfaces 310 which are in the form of electrically heated heating contacts, are close to one another and have a wavy construction and between them form a sinuous or undulating gap extending essentially from top to bottom. Within the gap between two sliding surfaces 310, a mixing movement is formed from a trickling of the raw meal 10 and a gas countercurrent, in which the raw meal 10, which is present with the already partially burnt or calcined lime 11, is swirled up in a manner similar to that in a countercurrent reactor. The gas countercurrent has a heat-recuperating effect which has already been discussed with respect to the embodiment of the plant in FIG. 2. It is important here that the distance between the second sliding surfaces 310 is not too wide, so that a separation between the trickling of the raw meal and the upward flow of the exhaust gas cannot occur. On the other hand, the distance must also not be so small that the raw meal 10 falls through a pipeline as if it were a pipe and rolls against the gas flowing up, so that the gas and the freely trickling raw meal 10 block the path alternately. The sliding surfaces 310 are connected on one side to resistance heaters 311. The gas flows upwards into the gas discharge in the head 304 of the reactor 305, whereas the completely burnt or calcined product falls into the foot 306 of the reactor 305. There the completely burnt or calcined lime is discharged through a cellular wheel sluice 313. The burnt or calcined lime 11 separated in the dust separator 307 is combined with the product originating from the cellular wheel sluice 313. The exhaust gas, on the other hand, flows via a flow regulator 314 and compressor 2316 to its further sequestration. \| [0021] Finally, FIG. 4 shows an installation 400 for the thermal treatment of raw meal 10 using an electric heating device 410 in a fourth embodiment. A screw conveyor 450 is arranged in the reactor 405, which is shown as a tubular reactor 405 horizontally or obliquely ("obliquely" not shown here). This screw conveyor 450 transports the raw meal 10 introduced into the reactor 405 via a cellular wheel sluice 401 via the sliding surfaces 410 which are let into the lower wall 451 and are electrically heated from below by resistance heaters 411. This embodiment has the advantage that the dwell time of the raw meal 10 on the sliding surfaces 410 can be set as an electrically heated heating contact with the speed of the screw conveyor 450. Vapors 415 and carbon dioxide (CO2) are also produced as waste gas in this reactor 405. This exhaust gas is passed via gas discharge lines 460 to a dust separator 412 which separates raw meal 11 still suspended in the exhaust gas from the exhaust gas. The remaining exhaust gas from vapors 415 and carbon dioxide (CO2) is then subjected to sequestration. On the other hand, the completely burnt or calcined product from the cellular wheel sluice is combined with the separated product from the dust separator 412.\| [0022] B E Z U G S Z E I C H E N L I S E \| [0023] Raw meal, unburnt 200 plant\| [0024] Raw flour, calcined 201 star feeder\| [0025] Raw meal, calcined 204 head (reactor) \| [0026] 205 Reactor\| [0027] Appendix 206 feet (reactor)\| [0028] Rotary valve 207 cyclone separator\| [0029] Heat exchanger 208 coarse material discharge\| [0030] Reactor 209 fines/gas outlet\| [0031] Foot (reactor) 210 sliding surface\| [0032] Cyclone separator 211 resistance heating\| [0033] Coarse material outlet 213 rotary valve\| [0034] Fine/gas outlet 214 flow controller\| [0035] Sliding surface 215 vapors\| [0036] Resistance heating 216 Compressor\| [0037] dust collector \| [0038] Cellular wheel lock 300 system\| [0039] Flow controller 301 rotary valve\| [0040] Vapors 304 head (reactor)\| [0041] Compressor 305 reactor \| [0042] 306 feet (reactor) sliding surface 414 flow regulator resistance heater 415 vapors cellular wheel sluice 416 compressor flow regulator 450 screw conveyor vapors 451 wall compressor 460 gas discharge system A detail cellular wheel sluice D partial roof surface dust separator	Family Number\|(115032330)\|115032330\|Object of Invention\|(DE102024102958 B3)\|It is therefore the object of the invention to provide a plant for the thermal treatment of lime in which exhaust gas purification before sequestration of the carbon dioxide (CO2_) can be dispensed with.\|(WO2025163040 A1)\|The aim of the invention is therefore to provide a method for thermally treating lime, in which exhaust gas purification prior to sequestration of the carbon dioxide (CO2) can be dispensed with. \|Advantages / Prev. Drawbacks\|(DE102024102958 B3)\| (...) The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive.\|(WO2025163040 A1)\| (...) The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive.\|	Materials, metallurgy\|Thermal processes and apparatus	C04B-002/12\|F27B-001/08\|F27D-011/02\|F27D-099/00/06		C04B-002/12\|F27B-001/08\|F27D-011/02\|F27D-099/00/06	C04B-002/10\|C04B-002/12\|F27B-001/08\|F27D-011/02\|F27D-099/00	C04B-002/10\|C04B-002/12\|F27B-001/08\|F27D-011/02\|F27D-099/00					US20240002288\|CN113149471\|US20210231374\|CN109133676\|CN103443046B\|DE102023202994\|DE4431508	US20240002288 100489638 WHO=Examiner SELF=N CAT=X CAT=I\|CN113149471 95339649 WHO=Examiner SELF=N CAT=X\|US20210231374 86865659 WHO=Examiner SELF=N CAT=X\|CN109133676 82881447 WHO=Examiner SELF=N CAT=X\|CN103443046B 7861390 WHO=Examiner SELF=N CAT=A\|DE102023202994 111675951 WHO=Examiner SELF=N\|DE4431508 13045774 WHO=Examiner SELF=N		US20240002288; CN113149471; CN109133676; US20210231374; CN103443046B\|DE4431508; DE102023202994	\|(DE102024102958)\|Search Report references [Examiner]\|-IBU tec: Der Drehrohrofen. URL: https://www.ibu-tec.de/anlagen/drehrohrofen/ [abgerufen am 16.10.2024]; vgl. auch http://web.archive.org/web/20230810231918/https://www.ibu-tec.de/anlagen/drehrohrofen/ (archiviert am 10.08.2023)i.V.m. Kalzinierung. URL: https://www.ibu-tec.de/expertise/prozesse/kalzinierung/ [abgerufen a, 16.10.2024]; vgl. auch https://web.archive.org/web/20231202013009/https://www.ibu-tec.de/expertise/prozesse/kalzinierung/ (archiviert am 02.12.2023)\|	GRANTED	(WO2025/163040)\|PENDING\|(DE102024102958)\|GRANTED	ALIVE	(WO2025/163040)\|ALIVE\|(DE102024102958)\|ALIVE	(WO2025/163040)\|LEGAL DETAILS FOR WO2025/163040\|Actual or expected expiration date=2027-08-02\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-01-30\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOEP2025/052349\|Application date=2025-01-30\|Standardized application number=2025WO-EP52349\|Event publication date=2025-08-07\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/163040\|Publication stage code=A1\|Publication date=2025-08-07\|Standardized publication number=WO2025163040\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2045-01-30\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP25702812\|Event publication date=2025-09-17\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|(DE102024102958)\|LEGAL DETAILS FOR DE102024102958\|Actual or expected expiration date=2044-02-02\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2024-02-02\|Event code=DE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=DE DE102024102958\|Application date=2024-02-02\|Standardized application number=2024DE-10102958\|Event publication date=2024-02-02\|Event code=DE/R012\|Event indicator=Pos\|Event group=Examination events\|Request for examination validly filed\|Pruefungsantrag wirksam gestellt\|Event publication date=2025-02-24\|Event code=DE/R016\|Event group=Examination events\|Response to examination communication\|Erwiderung auf pruefungsbescheid\|Event publication date=2025-03-17\|Event code=DE/R018\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant decision by examination section/examining division\|Erteilungsbeschluss durch pruefungsstelle/patentabteilung\|Event publication date=2025-06-26\|Event code=DE/B3\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent (First publication)\|Publication country=DE\|Publication number=DE102024102958\|Publication stage code=B3\|Publication date=2025-06-26\|Standardized publication number=DE102024102958	(WO2025/163040)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/163040)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/163040)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/163040)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/163040)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UY, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(WO2025/163040)\|WO; EP\|(DE102024102958)\|DE	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=icjTorqguCCYFl50vavvmN0P/F2Pwh1EkaV0SMUACwOCCKReMmHu7M9Ry4MrhQjLALkMBz8hwaI=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006833387&ekey=2608&xpn=WO2025163040&kind=A1	http://www.wipo.int/patentscope/search/en/detail.jsf?docId=WO2025163040&redirectedID=true	https://permalink.orbit.com/RenderStaticFirstPage?XPN=C8Srd52QghD6%252FxdSEPJ%252FabmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	DE	(WO2025/163040)\|DE\|(DE102024102958)\|DE	(WO2025/163040)\|NAME=KHD HUMBOLDT WEDAG GMBH Von-der-Wettern-Straße 4a 51149 Köln , COUNTRY=DE\|(DE102024102958)\|NAME=KHD Humboldt Wedag GmbH , CITY=Köln , POSTCODE=51067 , COUNTRY=DE			(WO2025/163040)\|DE; DE; DE\|(DE102024102958)\|DE; DE; DE	(WO2025/163040)\|NAME=FEISS, Marc Düsseldorfer Straße 125 51063 Köln, POSTCODE=51063, COUNTRY=DE \|NAME=KNOCH, Alexander Salgert 17 53797 Lohmar, POSTCODE=53797, COUNTRY=DE \|NAME=MERSMANN, Matthias Burgstraße 31 52222 Stolberg, POSTCODE=52222, COUNTRY=DE\|(DE102024102958)\|NAME=Mersmann Matthias, CITY=Stolberg, POSTCODE=52222, COUNTRY=DE \|NAME=Knoch Alexander, CITY=Lohmar, POSTCODE=53797, COUNTRY=DE \|NAME=Feiss Marc, CITY=Köln, POSTCODE=51063, COUNTRY=DE	(WO2025/163040)\|4\|(DE102024102958)\|1	1	2					(WO2025/163040)\|Number of Claims: NCL=8\|Extended kind: EXTK=x\|\|(DE102024102958)\|Number of Claims: NCL=4\|		(WO2025/163040)\|GERMAN (GER)	(WO2025163040)\|Patent\|(DE102024102958)\|Patent	Titre: (WO2025/163040)\|Method for the thermal treatment of raw meal using an electric heating device, and corresponding system Résumé: (WO2025/163040)\|The invention relates to a method for thermally treating raw meal in order to produce burnt lime and to a corresponding system. According to the invention, raw meal is thermally treated at an electrically heated heating contact. This leads to an exhaust gas which is free of nitrous gases and other organic constituents. The pure exhaust gas can be subjected to sequestration without any further special purification processes.	37	Abstract	gpt-4o-mini	no	The article focuses on thermal treatment for producing burnt lime and does not address accelerated weathering or CO₂ capture through mineral alteration.
39	EP11305696\|EP12727348\|WOEP2012/060480	WOEP2012/060480\|EP12727348\|HRP20180851T\|CN201280027687\|US14/123,987\|KR20137035129\|CA2838035\|EP11305696	HRP20180851\|EP2718230\|CN103582611\|US9469546\|US20140120022\|EP2718230\|KR10-2014-0045459\|CN103582611\|CA2838035\|WO2012/168176\|EP2532624	15065813	WO2012/168176 A1 2012-12-13 [WO2012168176]\|EP2718230 B1 2018-05-23 [EP2718230]\|EP2718230 A1 2014-04-16 [EP2718230]\|HRP20180851 T1 2018-06-29 [HRP20180851]\|CN103582611 B 2017-03-08 [CN103582611B]\|CN103582611 A 2014-02-12 [CN103582611]\|US9469546 B2 2016-10-18 [US9469546]\|US20140120022 A1 2014-05-01 [US20140120022]\|KR10-2014-0045459 A 2014-04-16 [KR20140045459]\|CA2838035 A1 2012-12-13 [CA2838035]\|EP2532624 A1 2012-12-12 [EP2532624]	2011-06-07\|2012-06-04	2012-06-04\|2012-06-04\|2012-06-04\|2012-06-04\|2012-06-04\|2012-06-04\|2012-06-04\|2011-06-07	2018-06-29\|2018-05-23\|2017-03-08\|2016-10-18\|2014-05-01\|2014-04-16\|2014-04-16\|2014-02-12\|2012-12-13\|2012-12-13\|2012-12-12	(EP2718230)\|2018-05-23\|\|(US9469546)\|2016-10-18\|\|(CN103582611B)\|2017-03-08\|(HRP20180851)\|2018-06-29\|\|	(EP2718230)\|2032-06-04\|(EP2532624)\|2017-07-15\|(US9469546)\|2020-11-23\|(WO2012/168176)\|2014-12-07\|(CN103582611)\|2019-06-04\|(HRP20180851)\|2019-06-04\|(KR10-2014-0045459)\|2017-07-05\|(CA2838035)\|2020-08-31	(EP2718230)\|Process for the mineralization of carbon dioxide	(EP2718230)\|The invention provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form, or in the form of an alkali metal carbonate or bicarbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.	HOLCIM TECHNOLOGY\|LAFARGE	(EP2718230)\|Lafarge ([FR])\|(EP2718230)\|Lafarge ([FR])\|(EP2532624)\|LAFARGE ([FR])\|(US9469546)\|LAFARGE ([FR])\|(US20140120022)\|LAFARGE ([FR])\|(WO2012/168176)\|LAFARGE ([FR])\|(CN103582611)\|LAFARGE SA ([FR])\|(CN103582611)\|LAFARGE SA ([FR])\|(HRP20180851)\|Lafarge\|(KR10-2014-0045459)\|LAFARGE\|(CA2838035)\|LAFARGE ([FR])	GARTNER ELLIS\|PISCH ALEXANDER	(EP2718230)\|GARTNER, Ellis\|PISCH, Alexander\|(EP2718230)\|GARTNER, Ellis\|PISCH, Alexander	(EP2718230)\|Keschmann, Marc;Haffner und Keschmann ([AT])\|Reg. Nb: 101393339\|(EP2532624)\|Mérigeault, Shona;Lafarge ([FR])\|Reg. Nb: 101004378\|(US9469546)\|Pillsbury Winthrop Shaw Pittman LLP\|(WO2012/168176)\|MERIGEAULT, Shona ([FR])\|(CN103582611)\|CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11314\|ZHU HUINING;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11314\|(KR10-2014-0045459)\|KOREANA PATENT FIRM\|Reg. Nb: 920011000013\|(CA2838035)\|NORTON ROSE FULBRIGHT CANADA LLP/S.E.N.C.R.L., S.R.L. ([CA])	(EP2718230)\|However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|It is therefore desirable to separate this alkali metal carbonate solution and extract the alkali metal carbonates in solid form for re-use in the high temperature process according to reaction (1).\|The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible.\|One of the major technical difficulties which renders such processes so expensive to set up and operate is the need to use elevated pressures and temperatures in order to achieve a sufficiently high rate (for industrial purposes) of carbonation of magnesium silicate minerals. Typically, the carbon dioxide gas must first be purified and then compressed to pressures in excess of 70 atmospheres, and then contacted with finely-ground magnesium silicates in a pressure reactor at temperatures of 120-200°C. This requires specialized equipment which is expensive to build and maintain, as well as large amounts of electric power to operate the gas purification and pressurization process as well as to finely grind the magnesium silicate rocks.\|	(EP2718230)\|1. A process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|	(EP2718230)\|The invention also provides a process for the preparation of a product comprising an alkali metal magnesium silicate compound (which compound is preferably of composition R2OMgOSiO2, (in which R represents an alkali metal),which process comprises the reaction, at a temperature from 500 to 1100°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 2:1 to 1:2, which reaction produces the product comprising an alkali metal magnesium silicate.\|The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. The present invention accordingly provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|This invention relates to a process for the mineralization of carbon dioxide from, for example, a gas stream such as the flue gases from an industrial combustion process.\|	(EP2718230)\|MAGNESIUM 2 CARBONATE(100,20)\|MAGNESIUM 2 CARBONATE COMPOUND(100,9)\|METHANEDIONE MINERALIZATION(100,5)\|METHANEDIONE CAPTURE(33,1)\|MAGNESIUM SILICATE(29,79)\|METHANEDIONE(26,25)\|MAGNESIUM SILICATE ROCK(22,6)\|ALKALI METAL CARBONATE(19,60)\|MAJOR TECHNICAL DIFFICULTY(19,1)\|OUTGOING HOT GAS(19,1)\|PRECONCENTRATION(19,1)\|MOVING GRATE FURNACE(18,2)\|SPECIALIZED EQUIPMENT(18,1)\|ALKALI METAL(17,115)\|ALKALI METAL BICARBONATE(17,10)\|OUTGOING HOT SOLID(17,1)\|ALKALI METAL MAGNESIUM SILICATE(16,33)\|GAS PURIFICATION(16,1)\|FURNACE(14,4)\|MAGNESIUM SILICATE MINERAL(14,3)\|INCOMING SOLID(14,1)\|PRESSURIZING(14,1)\|METHANEDIONE GAS(13,4)\|FINELY GROUND MAGNESIUM SILICATE(13,1)\|MOLAR RATIO(12,6)\|CARBONATION(12,2)\|MOVING GRATE(11,5)\|INCOMING COMBUSTION AIR(11,1)\|COUNTERCURRENT HEAT EXCHANGE(10,3)\|NET ENERGY CONSUMPTION(10,2)\|COOLED DECARBONATED PELLET(9,4)\|PELLET(8,14)\|SIO(8,5)\|GAS STREAM(8,3)\|CO2(7,18)\|MGO(7,13)\|PRESSURE ELEVATION(7,3)\|COMBUSTION(7,2)\|FLUE GAS(6,7)\|GAS SCRUBBING(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|PREHEATER CYCLONE TOWER(6,1)\|HYDROMAGNESITE(5,10)\|ALKALI METAL HYDROXIDE(5,3)\|LAB FURNACE(5,3)\|EARTH CRUST(5,2)\|LASER GRANULOMETRY(5,2)\|PLATINUM CRUCIBLE(5,2)\|UNREACTED OLIVINE(5,2)\|ASBESTOS FIBRILLAR(5,1)\|DECARBONATED NODULE(5,1)\|OBSCURATION STABILIZATION(5,1)\|MG2SIO(4,6)\|FORSTERITE(4,5)\|AMORPHOUS PRODUCT(4,4)\|ENERGY EFFICIENCY(4,3)\|ANHYDROUS MAGNESIUM SILICATE(4,2)\|DECARBONATION REACTION(4,2)\|EXCESS METHANEDIONE(4,2)\|PRESSURE REACTOR(4,2)\|ABSORB METHANEDIONE(4,1)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|GASEOUS METHANEDIONE(4,1)\|HEAT TRANSFER(4,1)\|HELICOIDAL TEFLON(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|PREHEATER TOWER(4,1)\|REACTION PRODUCT(3,7)\|ATMOSPHERIC PRESSURE(3,5)\|PARTICULATE(3,5)\|FILTER CAKE DRYING(3,3)\|FUEL COMBUSTION GAS(3,3)\|NITRITE(3,3)\|BURNING ZONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|GASEOUS CO2(3,2)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GROUND OLIVINE MIX(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SUSPENSION PREHEATER(3,1)\|TALC IDDINGSITE(3,1)\|ALKALI METAL OXIDE(2,6)\|AQUEOUS SOLUTION(2,4)\|EXPERIMENT(2,4)\|HOT GAS(2,4)\|R2CO(2,4)\|ROTARY KILN(2,4)\|AQUEOUS SUSPENSION(2,3)\|MGCO(2,3)\|STOICHIOMETRIC RATIO(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANHYDROUS PRODUCT(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|MEASURED LOI DATA(2,2)\|MIXED POWDER(2,2)\|PYROXENE(2,2)\|SIEVING(2,2)\|SODIUM CARBONATE POWDER(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|ALKALINE FLUX(2,1)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CO2 GRAM(2,1)\|COMBINED CO2 QUANTITATIVE DETECTION(2,1)\|CRUSHED SAMPLE(2,1)\|DISSOLVED BICARBONATE SALT(2,1)\|EARTH MANTLE COMPONENT(2,1)\|ESTIMATED MG(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE NESS(2,1)\|FINE SAND GRANULOMETRY(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|MAXIMUM CO2 CAPTURE(2,1)\|MAXIMUM SLURRY ADDITIVE(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|NONTOXIC WASTE(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|PELLET R2O SILICA RATIO(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|QUALITATIVE PHASE(2,1)\|R2O MOLAR RATIO(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SILICATE HYDROXIDE(2,1)\|SKIN CLEANING(2,1)\|SLURRY CONC(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|STEEL CRUCIBLE(2,1)\|SULFUR CONTENT(2,1)\|SUSPENSION AGITATION(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|ADSORPTION(1,1)\|AMORPHOUS SOLID RICH(1,1)\|ANALYZING IMAGE(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BICARBONATE SOLUTION(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CAO SILICA MOLAR RATIO(1,1)\|CARBONATE PRODUCT(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|CONVERSION YIELD(1,1)\|COUNTERCURRENT(1,1)\|CRYSTALLINE PHASE(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FEO SILICA MOLAR RATIO(1,1)\|FILTER CAKE MG(1,1)\|FILTERCAKE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GLASS REACTOR(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT WATER CIRCULATION(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|HYPERSTHENE(1,1)\|INCOMING AIR(1,1)\|LIQUID FILTRATE(1,1)\|LITHIUM MAGNESIUM SODIUM SILICATE(1,1)\|\|(EP2718230)\|MAGNESIUM 2 CARBONATE(100,20)\|MAGNESIUM 2 CARBONATE COMPOUND(100,9)\|METHANEDIONE MINERALIZATION(100,5)\|METHANEDIONE CAPTURE(33,1)\|MAGNESIUM SILICATE(29,79)\|METHANEDIONE(26,25)\|MAGNESIUM SILICATE ROCK(22,6)\|ALKALI METAL CARBONATE(19,60)\|MAJOR TECHNICAL DIFFICULTY(19,1)\|OUTGOING HOT GAS(19,1)\|PRECONCENTRATION(19,1)\|MOVING GRATE FURNACE(18,2)\|SPECIALIZED EQUIPMENT(18,1)\|ALKALI METAL(17,115)\|ALKALI METAL BICARBONATE(17,10)\|OUTGOING HOT SOLID(17,1)\|ALKALI METAL MAGNESIUM SILICATE(16,33)\|GAS PURIFICATION(16,1)\|FURNACE(14,4)\|MAGNESIUM SILICATE MINERAL(14,3)\|INCOMING SOLID(14,1)\|PRESSURIZING(14,1)\|METHANEDIONE GAS(13,4)\|FINELY GROUND MAGNESIUM SILICATE(13,1)\|MOLAR RATIO(12,6)\|CARBONATION(12,2)\|MOVING GRATE(11,5)\|INCOMING COMBUSTION AIR(11,1)\|COUNTERCURRENT HEAT EXCHANGE(10,3)\|NET ENERGY CONSUMPTION(10,2)\|COOLED DECARBONATED PELLET(9,4)\|PELLET(8,14)\|SIO(8,5)\|GAS STREAM(8,3)\|CO2(7,18)\|MGO(7,13)\|PRESSURE ELEVATION(7,3)\|COMBUSTION(7,2)\|FLUE GAS(6,7)\|GAS SCRUBBING(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|PREHEATER CYCLONE TOWER(6,1)\|HYDROMAGNESITE(5,10)\|ALKALI METAL HYDROXIDE(5,3)\|LAB FURNACE(5,3)\|EARTH CRUST(5,2)\|LASER GRANULOMETRY(5,2)\|PLATINUM CRUCIBLE(5,2)\|UNREACTED OLIVINE(5,2)\|ASBESTOS FIBRILLAR(5,1)\|DECARBONATED NODULE(5,1)\|OBSCURATION STABILIZATION(5,1)\|MG2SIO(4,6)\|FORSTERITE(4,5)\|AMORPHOUS PRODUCT(4,4)\|ENERGY EFFICIENCY(4,3)\|ANHYDROUS MAGNESIUM SILICATE(4,2)\|DECARBONATION REACTION(4,2)\|EXCESS METHANEDIONE(4,2)\|PRESSURE REACTOR(4,2)\|ABSORB METHANEDIONE(4,1)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|GASEOUS METHANEDIONE(4,1)\|HEAT TRANSFER(4,1)\|HELICOIDAL TEFLON(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|PREHEATER TOWER(4,1)\|REACTION PRODUCT(3,7)\|ATMOSPHERIC PRESSURE(3,5)\|PARTICULATE(3,5)\|FILTER CAKE DRYING(3,3)\|FUEL COMBUSTION GAS(3,3)\|NITRITE(3,3)\|BURNING ZONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|GASEOUS CO2(3,2)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GROUND OLIVINE MIX(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SUSPENSION PREHEATER(3,1)\|TALC IDDINGSITE(3,1)\|ALKALI METAL OXIDE(2,6)\|AQUEOUS SOLUTION(2,4)\|EXPERIMENT(2,4)\|HOT GAS(2,4)\|R2CO(2,4)\|ROTARY KILN(2,4)\|AQUEOUS SUSPENSION(2,3)\|MGCO(2,3)\|STOICHIOMETRIC RATIO(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANHYDROUS PRODUCT(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|MEASURED LOI DATA(2,2)\|MIXED POWDER(2,2)\|PYROXENE(2,2)\|SIEVING(2,2)\|SODIUM CARBONATE POWDER(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|ALKALINE FLUX(2,1)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CO2 GRAM(2,1)\|COMBINED CO2 QUANTITATIVE DETECTION(2,1)\|CRUSHED SAMPLE(2,1)\|DISSOLVED BICARBONATE SALT(2,1)\|EARTH MANTLE COMPONENT(2,1)\|ESTIMATED MG(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE NESS(2,1)\|FINE SAND GRANULOMETRY(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|MAXIMUM CO2 CAPTURE(2,1)\|MAXIMUM SLURRY ADDITIVE(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|NONTOXIC WASTE(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|PELLET R2O SILICA RATIO(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|QUALITATIVE PHASE(2,1)\|R2O MOLAR RATIO(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SILICATE HYDROXIDE(2,1)\|SKIN CLEANING(2,1)\|SLURRY CONC(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|STEEL CRUCIBLE(2,1)\|SULFUR CONTENT(2,1)\|SUSPENSION AGITATION(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|ADSORPTION(1,1)\|AMORPHOUS SOLID RICH(1,1)\|ANALYZING IMAGE(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BICARBONATE SOLUTION(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CAO SILICA MOLAR RATIO(1,1)\|CARBONATE PRODUCT(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|CONVERSION YIELD(1,1)\|COUNTERCURRENT(1,1)\|CRYSTALLINE PHASE(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FEO SILICA MOLAR RATIO(1,1)\|FILTER CAKE MG(1,1)\|FILTERCAKE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GLASS REACTOR(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT WATER CIRCULATION(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|HYPERSTHENE(1,1)\|INCOMING AIR(1,1)\|LIQUID FILTRATE(1,1)\|LITHIUM MAGNESIUM SODIUM SILICATE(1,1)\|\|(EP2532624)\|MAGNESIUM 2 CARBONATE(100,22)\|MAGNESIUM 2 CARBONATE COMPOUND(100,11)\|METHANEDIONE MINERALIZATION(100,6)\|METHANEDIONE CAPTURE(30,1)\|MAGNESIUM SILICATE(28,78)\|METHANEDIONE(27,22)\|MAGNESIUM SILICATE ROCK(20,6)\|ALKALI METAL CARBONATE(18,59)\|PRECONCENTRATION(18,1)\|ALKALI METAL MAGNESIUM SILICATE(17,34)\|MAJOR TECHNICAL DIFFICULTY(17,1)\|OUTGOING HOT GAS(17,1)\|ALKALI METAL(16,115)\|ALKALI METAL BICARBONATE(16,10)\|MOVING GRATE FURNACE(16,2)\|SPECIALIZED EQUIPMENT(16,1)\|OUTGOING HOT SOLID(15,1)\|GAS PURIFICATION(14,1)\|FURNACE(13,4)\|MAGNESIUM SILICATE MINERAL(13,3)\|INCOMING SOLID(13,1)\|PRESSURIZING(13,1)\|METHANEDIONE GAS(12,4)\|FINELY GROUND MAGNESIUM SILICATE(12,1)\|MOLAR RATIO(11,6)\|BICARBONATE(11,5)\|CARBONATION(11,2)\|MOVING GRATE(10,5)\|NET ENERGY CONSUMPTION(10,2)\|INCOMING COMBUSTION AIR(10,1)\|COUNTERCURRENT HEAT EXCHANGE(9,3)\|PRESSURE ELEVATION(9,1)\|PELLET(8,14)\|COOLED DECARBONATED PELLET(8,4)\|GAS STREAM(8,3)\|MGO(7,8)\|SIO(7,6)\|CO2(6,16)\|FLUE GAS(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|COMBUSTION(6,2)\|ALKALI METAL SILICATE(6,1)\|PREHEATER CYCLONE TOWER(6,1)\|GAS SCRUBBING(5,7)\|UNREACTED OLIVINE(5,2)\|MG2SIO(4,7)\|ALKALI METAL HYDROXIDE(4,3)\|EARTH CRUST(4,2)\|LASER GRANULOMETRY(4,2)\|PLATINUM CRUCIBLE(4,2)\|ASBESTOS FIBRILLAR(4,1)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|DECARBONATED NODULE(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|OBSCURATION STABILIZATION(4,1)\|FORSTERITE(3,5)\|HYDROMAGNESITE(3,5)\|ATMOSPHERIC PRESSURE(3,4)\|PARTICULATE(3,4)\|ENERGY EFFICIENCY(3,3)\|R2MGSIO(3,3)\|ANHYDROUS MAGNESIUM SILICATE(3,2)\|BURNING ZONE(3,2)\|EXCESS METHANEDIONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|GASEOUS CO2(3,2)\|LAB FURNACE(3,2)\|PRESSURE REACTOR(3,2)\|ABSORB METHANEDIONE(3,1)\|CO2 HINGE(3,1)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GASEOUS METHANEDIONE(3,1)\|GROUND OLIVINE MIX(3,1)\|HEAT TRANSFER(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|PREHEATER TOWER(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SUSPENSION PREHEATER(3,1)\|ALKALI METAL OXIDE(2,6)\|REACTION PRODUCT(2,5)\|AQUEOUS SOLUTION(2,4)\|HOT GAS(2,4)\|R2CO(2,4)\|ROTARY KILN(2,4)\|FUEL COMBUSTION GAS(2,3)\|NITRITE(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|FILTERCAKE(2,2)\|MEASURED LOI DATA(2,2)\|PYROXENE(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CO2 GRAM(2,1)\|DECARBONATION REACTION(2,1)\|EARTH MANTLE COMPONENT(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE PRECIPITATE(2,1)\|FINE SAND GRANULOMETRY(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|MAXIMUM CO2 CAPTURE(2,1)\|MAXIMUM SLURRY ADDITIVE(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MICROCRYSTALLINE SILICA PRODUCT(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|PELLET R2O SILICA RATIO(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|R2O MOLAR RATIO(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SLURRY CONC(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|SULFUR CONTENT(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|MGCO(1,3)\|STOICHIOMETRIC RATIO(1,3)\|EXPERIMENT(1,2)\|ANALYZING IMAGE(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CAO SILICA MOLAR RATIO(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|COUNTERCURRENT(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FEO SILICA MOLAR RATIO(1,1)\|FILTRATE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|HYPERSTHENE(1,1)\|IDDINGSITE(1,1)\|INCOMING AIR(1,1)\|LIZARDITE(1,1)\|\|(US9469546)\|MAGNESIUM 2 CARBONATE(100,21)\|MAGNESIUM 2 CARBONATE COMPOUND(100,10)\|METHANEDIONE MINERALIZATION(100,6)\|MAGNESIUM SILICATE(39,77)\|MOLAR RATIO(32,8)\|METHANEDIONE(30,22)\|ALKALI METAL CARBONATE(29,58)\|COMPOSITION R2O(26,1)\|MAJOR TECHNICAL DIFFICULTY(25,1)\|OUTGOING HOT GAS(25,1)\|ALKALI METAL(24,112)\|MOVING GRATE FURNACE(24,2)\|SPECIALIZED EQUIPMENT(24,1)\|OUTGOING HOT SOLID(23,1)\|ALKALI METAL MAGNESIUM SILICATE(21,32)\|GAS PURIFICATION(21,1)\|ALKALI METAL BICARBONATE(19,9)\|MAGNESIUM SILICATE ROCK(19,6)\|FURNACE(19,4)\|MAGNESIUM SILICATE MINERAL(19,3)\|INCOMING SOLID(19,1)\|PRESSURIZING(19,1)\|METHANEDIONE GAS(18,4)\|FINELY GROUND MAGNESIUM SILICATE(17,1)\|CARBONATION(16,2)\|MOVING GRATE(15,5)\|INCOMING COMBUSTION AIR(15,1)\|COUNTERCURRENT HEAT EXCHANGE(14,3)\|NET ENERGY CONSUMPTION(14,2)\|COOLED DECARBONATED PELLET(12,4)\|PELLET(11,14)\|MGO(11,11)\|SIO(11,5)\|MINERAL(10,8)\|SLURRY(9,10)\|BED(9,5)\|PRESSURE ELEVATION(9,3)\|GAS SCRUBBING(8,7)\|HEAT EXCHANGE(8,4)\|PREHEATER CYCLONE TOWER(8,1)\|UNREACTED OLIVINE(7,2)\|ASBESTOS FIBRILLAR(7,1)\|DECARBONATED NODULE(7,1)\|OBSCURATION STABILIZATION(7,1)\|MG2SIO(6,7)\|AMORPHOUS PRODUCT(6,4)\|ALKALI METAL HYDROXIDE(6,3)\|LAB FURNACE(6,3)\|EARTH CRUST(6,2)\|LASER GRANULOMETRY(6,2)\|PLATINUM CRUCIBLE(6,2)\|CO2 MAXIMIZING CAPTURE(6,1)\|COUNTER CURRENT HEAT EXCHANGE(6,1)\|METHANEDIONE CAPTURE(6,1)\|METHANEDIONE GAS LIBERATION(6,1)\|HYDROMAGNESITE(5,6)\|FORSTERITE(5,5)\|PARTICULATE(5,5)\|ENERGY EFFICIENCY(5,3)\|ANHYDROUS MAGNESIUM SILICATE(5,2)\|BURNING ZONE(5,2)\|DECARBONATION REACTION(5,2)\|EXCESS METHANEDIONE(5,2)\|GASEOUS CO2(5,2)\|PRESSURE REACTOR(5,2)\|SLURRY ADDITIVE(5,2)\|ABSORB METHANEDIONE(5,1)\|CO2 SLURRY(5,1)\|GASEOUS METHANEDIONE(5,1)\|HEAT TRANSFER(5,1)\|HELICOIDAL TEFLON(5,1)\|PREHEATER TOWER(5,1)\|REACTION PRODUCT(4,7)\|ALKALI METAL OXIDE(4,6)\|FUEL COMBUSTION GAS(4,3)\|NITRITE(4,3)\|GAS ABSORBER COLUMN(4,2)\|COMPOSITION OLIVINE SAND(4,1)\|CRYSTALIZATION SPECIALIZATION(4,1)\|GROUND OLIVINE MIX(4,1)\|LASER GRANULOMETER(4,1)\|MAGNESIUM SILICATE CARBONATION(4,1)\|MAXIMIZATION(4,1)\|MAXIMIZE CAPTURE(4,1)\|SAMPLE DEAGGLOMERATION(4,1)\|SLURRY TEMP(4,1)\|SUSPENSION PREHEATER(4,1)\|R2CO(3,5)\|AQUEOUS SOLUTION(3,4)\|HOT GAS(3,4)\|ROTARY KILN(3,4)\|ACTINOLITE(3,2)\|AMOSITE(3,2)\|AMPHIBOLE(3,2)\|ANTHOPHYLLITE(3,2)\|CHLORITE(3,2)\|CHRYSOTILE(3,2)\|ENSTATITE(3,2)\|MEASURED LOI DATA(3,2)\|MIXED POWDER(3,2)\|PYROXENE(3,2)\|R2MGSIO(3,2)\|SIEVING(3,2)\|SULFITE(3,2)\|TREMOLITE(3,2)\|ULTRASOUND(3,2)\|ANHYDROUS DURATION PRODUCT(3,1)\|BASIC MAGNESIUM ORTHOSILICATE(3,1)\|BIOMASS DERIVED FUEL(3,1)\|BLUE DIODE(3,1)\|CALCULATION MATRIX(3,1)\|CARBONATABLE SOLID(3,1)\|CO2 GRAM(3,1)\|COMBINED CO2 QUANTITATIVE DETECTION(3,1)\|CRUSHED SAMPLE(3,1)\|EARTH MANTLE COMPONENT(3,1)\|ESTIMATED MG(3,1)\|EXPERIMENT CAPTURED VOLUME(3,1)\|FERMENTATION RESIDUE GAS(3,1)\|FINE NESS(3,1)\|FINE SAND GRANULOMETRY(3,1)\|GAS SCRUBBER(3,1)\|HOT NODULE HEAT(3,1)\|INCOMING COMBUSTION AIR PREHEATER(3,1)\|INORGANIC IMPURITY(3,1)\|MAXIMUM CO2 CAPTURE(3,1)\|METHANEDIONE GAS ACTION(3,1)\|MINERALIZATION(3,1)\|MOVING GRATE COOLER(3,1)\|NATURALLY OCCURRING MINERAL(3,1)\|OLIVINE SAMPLE(3,1)\|OUTGOING SOLID PARTICLE(3,1)\|PACKED BED COLUMN(3,1)\|PELLET R2O SILICA RATIO(3,1)\|POROUS BED(3,1)\|POWDER SELF NODULIZE(3,1)\|PRECONCENTRATION(3,1)\|PREHEATER TOP CYCLONE(3,1)\|QUALITATIVE PHASE(3,1)\|R2O MOLAR RATIO(3,1)\|REACTED SAMPLE PHASE CONSTITUTION(3,1)\|REACTION ESCAPE(3,1)\|RED HE NE LASER(3,1)\|SAMPLE REACTION(3,1)\|SCRUBBING FLUE GAS(3,1)\|SESQUIHYDRATE(3,1)\|SILICA MOLE(3,1)\|SOLID PRECIPITATION(3,1)\|SOLUBLE SALT(3,1)\|STABLE NODULE(3,1)\|STEEL CRUCIBLE(3,1)\|SULFUR CONTENT(3,1)\|SUSPENSION AGITATION(3,1)\|UNREACTED MAGNESIUM SILICATE(3,1)\|WORKING SESSION(3,1)\|AQUEOUS SUSPENSION(2,3)\|STOICHIOMETRIC RATIO(2,3)\|GAS STREAM(2,2)\|ADSORPTION(2,1)\|ANALYZING IMAGE(2,1)\|ANHYDROUS PRODUCT(2,1)\|ANHYDROUS SODIUM CARBONATE(2,1)\|ANTIGORITE(2,1)\|AQUEOUS ACID(2,1)\|AUTOCLAVE(2,1)\|BASIC MAGNESIUM SILICATE(2,1)\|BRONZITE(2,1)\|BURNER(2,1)\|CALCINATION(2,1)\|CAO SILICA MOLAR RATIO(2,1)\|CARBONATE PRODUCT(2,1)\|CHONDRODITE(2,1)\|CLOSED REACTOR(2,1)\|COMPLEX MAGNESIUM(2,1)\|CONVERSION YIELD(2,1)\|COUNTERCURRENT(2,1)\|DECAHYDRATE(2,1)\|DECARBONATION DEGREE(2,1)\|DECOMPOSITION(2,1)\|DIHYDRATE(2,1)\|DIOPSIDE(2,1)\|EXPRESSED REACTION(2,1)\|FAYALITE(2,1)\|FE2SIO(2,1)\|FEO SILICA MOLAR RATIO(2,1)\|FILTER CAKE DRYING(2,1)\|FILTERCAKE(2,1)\|FINE POWDER(2,1)\|GARNIERITE(2,1)\|GLASS REACTOR(2,1)\|GRANULE(2,1)\|HECTORITE(2,1)\|HOT WATER CIRCULATION(2,1)\|HOT ZONE(2,1)\|HUMITE(2,1)\|HYPERSTHENE(2,1)\|IDDINGSITE(2,1)\|INCOMING AIR(2,1)\|LIQUID FILTRATE(2,1)\|LIZARDITE(2,1)\|\|(US20140120022)\|MAGNESIUM 2 CARBONATE(100,22)\|MAGNESIUM 2 CARBONATE COMPOUND(100,11)\|METHANEDIONE MINERALIZATION(100,6)\|MAGNESIUM SILICATE(31,82)\|METHANEDIONE CAPTURE(31,1)\|METHANEDIONE(27,23)\|MAGNESIUM SILICATE ROCK(21,6)\|ALKALI METAL CARBONATE(19,60)\|ALKALI METAL(18,119)\|ALKALI METAL MAGNESIUM SILICATE(18,37)\|COMPOSITION R2O(18,1)\|MAJOR TECHNICAL DIFFICULTY(18,1)\|OUTGOING HOT GAS(18,1)\|PRECONCENTRATION(18,1)\|MOVING GRATE FURNACE(17,2)\|SPECIALIZED EQUIPMENT(17,1)\|ALKALI METAL BICARBONATE(16,10)\|FORMULA SI SILICA(16,1)\|OUTGOING HOT SOLID(16,1)\|GAS PURIFICATION(15,1)\|PRESSURIZING(14,1)\|FURNACE(13,4)\|MAGNESIUM SILICATE MINERAL(13,3)\|INCOMING SOLID(13,1)\|METHANEDIONE GAS(12,4)\|FINELY GROUND MAGNESIUM SILICATE(12,1)\|MOLAR RATIO(11,6)\|CARBONATION(11,2)\|MOVING GRATE(10,5)\|COUNTERCURRENT HEAT EXCHANGE(10,3)\|NET ENERGY CONSUMPTION(10,2)\|INCOMING COMBUSTION AIR(10,1)\|COOLED DECARBONATED PELLET(9,4)\|PELLET(8,14)\|GAS STREAM(8,3)\|CO2(7,19)\|MGO(7,12)\|COMBUSTION(7,2)\|FLUE GAS(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|SIO(6,4)\|PRESSURE ELEVATION(6,3)\|PREHEATER CYCLONE TOWER(6,1)\|GAS SCRUBBING(5,7)\|UNREACTED OLIVINE(5,2)\|ASBESTOS FIBRILLAR(5,1)\|DECARBONATED NODULE(5,1)\|OBSCURATION STABILIZATION(5,1)\|HYDROMAGNESITE(4,6)\|MG2SIO(4,6)\|FORSTERITE(4,5)\|AMORPHOUS PRODUCT(4,4)\|ALKALI METAL HYDROXIDE(4,3)\|LAB FURNACE(4,3)\|EARTH CRUST(4,2)\|LASER GRANULOMETRY(4,2)\|PLATINUM CRUCIBLE(4,2)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|ATMOSPHERIC PRESSURE(3,5)\|PARTICULATE(3,5)\|ENERGY EFFICIENCY(3,3)\|ANHYDROUS MAGNESIUM SILICATE(3,2)\|BURNING ZONE(3,2)\|DECARBONATION REACTION(3,2)\|EXCESS METHANEDIONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|GASEOUS CO2(3,2)\|PRESSURE REACTOR(3,2)\|SLURRY ADDITIVE(3,2)\|ABSORB METHANEDIONE(3,1)\|CO2 SLURRY(3,1)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GASEOUS METHANEDIONE(3,1)\|GROUND OLIVINE MIX(3,1)\|HEAT TRANSFER(3,1)\|HELICOIDAL TEFLON(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|PREHEATER TOWER(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SLURRY TEMP(3,1)\|SUSPENSION PREHEATER(3,1)\|REACTION PRODUCT(2,7)\|ALKALI METAL OXIDE(2,6)\|AQUEOUS SOLUTION(2,4)\|HOT GAS(2,4)\|R2CO(2,4)\|ROTARY KILN(2,4)\|FUEL COMBUSTION GAS(2,3)\|NITRITE(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|MEASURED LOI DATA(2,2)\|MIXED POWDER(2,2)\|PYROXENE(2,2)\|SIEVING(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|ANHYDROUS DURATION PRODUCT(2,1)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CO2 GRAM(2,1)\|COMBINED CO2 QUANTITATIVE DETECTION(2,1)\|CRUSHED SAMPLE(2,1)\|EARTH MANTLE COMPONENT(2,1)\|ESTIMATED MG(2,1)\|EXPERIMENT CAPTURED VOLUME(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE NESS(2,1)\|FINE SAND GRANULOMETRY(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|MAXIMUM CO2 CAPTURE(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|PELLET R2O SILICA RATIO(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|QUALITATIVE PHASE(2,1)\|R2O MOLAR RATIO(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|STEEL CRUCIBLE(2,1)\|SULFUR CONTENT(2,1)\|SUSPENSION AGITATION(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|AQUEOUS SUSPENSION(1,3)\|STOICHIOMETRIC RATIO(1,3)\|ADSORPTION(1,1)\|AMORPHOUS SOLID RICH(1,1)\|ANALYZING IMAGE(1,1)\|ANHYDROUS PRODUCT(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CAO SILICA MOLAR RATIO(1,1)\|CARBONATE PRODUCT(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|CONVERSION YIELD(1,1)\|COUNTERCURRENT(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|EXPRESSED REACTION(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FEO SILICA MOLAR RATIO(1,1)\|FILTER CAKE DRYING(1,1)\|FILTERCAKE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GLASS REACTOR(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT WATER CIRCULATION(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|HYPERSTHENE(1,1)\|IDDINGSITE(1,1)\|INCOMING AIR(1,1)\|\|(WO2012/168176)\|MAGNESIUM 2 CARBONATE(100,18)\|MAGNESIUM 2 CARBONATE COMPOUND(100,9)\|METHANEDIONE MINERALIZATION(100,5)\|METHANEDIONE CAPTURE(49,1)\|MAGNESIUM SILICATE(47,81)\|METHANEDIONE(39,22)\|MAGNESIUM SILICATE ROCK(32,6)\|FORMULA SI(30,2)\|ALKALI METAL CARBONATE(29,59)\|MAJOR TECHNICAL DIFFICULTY(28,1)\|OUTGOING HOT GAS(28,1)\|PRECONCENTRATION(28,1)\|ALKALI METAL(27,117)\|ALKALI METAL MAGNESIUM SILICATE(27,36)\|MOVING GRATE FURNACE(27,2)\|SPECIALIZED EQUIPMENT(27,1)\|ALKALI METAL BICARBONATE(26,10)\|FORMULA SI SILICA(25,1)\|OUTGOING HOT SOLID(25,1)\|GAS PURIFICATION(23,1)\|FURNACE(21,4)\|MAGNESIUM SILICATE MINERAL(21,3)\|INCOMING SOLID(21,1)\|PRESSURIZING(21,1)\|METHANEDIONE GAS(20,4)\|FINELY GROUND MAGNESIUM SILICATE(19,1)\|CARBONATION(17,2)\|MOLAR RATIO(16,9)\|MOVING GRATE(16,5)\|NET ENERGY CONSUMPTION(16,2)\|INCOMING COMBUSTION AIR(16,1)\|COUNTERCURRENT HEAT EXCHANGE(15,3)\|COOLED DECARBONATED PELLET(14,4)\|GAS STREAM(13,3)\|PELLET(12,14)\|MGO(11,10)\|COMBUSTION(11,2)\|BED(10,5)\|PRESSURE ELEVATION(10,3)\|FLUE GAS(9,7)\|GAS SCRUBBING(9,7)\|HEAT EXCHANGE(9,4)\|PREHEATER CYCLONE TOWER(9,1)\|LARGELY AMORPHOUS PRODUCT CERAMICS(8,4)\|UNREACTED OLIVINE(8,2)\|ALKALI METAL HYDROXIDE(7,3)\|LAB FURNACE(7,3)\|EARTH CRUST(7,2)\|LASER GRANULOMETRY(7,2)\|PLATINUM CRUCIBLE(7,2)\|ASBESTOS FIBRILLAR(7,1)\|COUNTER CURRENT HEAT EXCHANGE(7,1)\|DECARBONATED NODULE(7,1)\|METHANEDIONE GAS LIBERATION(7,1)\|OBSCURATION STABILIZATION(7,1)\|FORSTERITE(6,5)\|ENERGY EFFICIENCY(6,3)\|ANHYDROUS MAGNESIUM SILICATE(6,2)\|DECARBONATION REACTION(6,2)\|EXCESS METHANEDIONE(6,2)\|PRESSURE REACTOR(6,2)\|SLURRY ADDITIVE(6,2)\|ABSORB METHANEDIONE(6,1)\|GASEOUS METHANEDIONE(6,1)\|HEAT TRANSFER(6,1)\|HELICOIDAL TEFLON(6,1)\|PREHEATER TOWER(6,1)\|ATMOSPHERIC PRESSURE(5,5)\|PARTICULATE(5,5)\|BURNING ZONE(5,2)\|COMPOSITION OLIVINE SAND(5,1)\|CRYSTALIZATION SPECIALIZATION(5,1)\|LASER GRANULOMETER(5,1)\|MAGNESIUM SILICATE CARBONATION(5,1)\|MAXIMIZE CAPTURE(5,1)\|SAMPLE DEAGGLOMERATION(5,1)\|SUSPENSION PREHEATER(5,1)\|MG2SI(4,7)\|REACTION PRODUCT(4,7)\|FUEL COMBUSTION GAS(4,3)\|HYDROMAGNESITE(4,3)\|NITRITE(4,3)\|R2MGSI(4,3)\|GAS ABSORBER COLUMN(4,2)\|EARTH MANTLE COMPONENT(4,1)\|FERMENTATION RESIDUE GAS(4,1)\|FINE NESS(4,1)\|FINE SAND GRANULOMETRY(4,1)\|INORGANIC IMPURITY(4,1)\|LN EXPERIMENT(4,1)\|MOVING GRATE COOLER(4,1)\|OLIVINE SAMPLE(4,1)\|PACKED BED COLUMN(4,1)\|QUANTITATIVE DETECTION(4,1)\|STABLE NODULE(4,1)\|SUSPENSION AGITATION(4,1)\|UNREACTED MAGNESIUM SILICATE(4,1)\|WORKING SESSION(4,1)\|ALKALI METAL OXIDE(3,6)\|R2C(3,5)\|AQUEOUS SOLUTION(3,4)\|HOT GAS(3,4)\|MGC(3,4)\|ROTARY KILN(3,4)\|AQUEOUS SUSPENSION(3,3)\|STOICHIOMETRIC RATIO(3,3)\|ACTINOLITE(3,2)\|AMOSITE(3,2)\|AMPHIBOLE(3,2)\|ANTHOPHYLLITE(3,2)\|CHLORITE(3,2)\|CHRYSOTILE(3,2)\|ENSTATITE(3,2)\|MEASURED LOI DATA(3,2)\|MIXED POWDER(3,2)\|PYROXENE(3,2)\|SIEVING(3,2)\|SULFITE(3,2)\|TREMOLITE(3,2)\|ULTRASOUND(3,2)\|BASIC MAGNESIUM ORTHOSILICATE(3,1)\|BIOMASS DERIVED FUEL(3,1)\|BLUE DIODE(3,1)\|CALCULATION MATRIX(3,1)\|CARBONATABLE SOLID(3,1)\|CRUSHED SAMPLE(3,1)\|GAS SCRUBBER(3,1)\|HOT NODULE HEAT(3,1)\|INCOMING COMBUSTION AIR PREHEATER(3,1)\|METHANEDIONE GAS ACTION(3,1)\|MINERALIZATION(3,1)\|NATURALLY OCCURRING MINERAL(3,1)\|OUTGOING SOLID PARTICLE(3,1)\|POROUS BED(3,1)\|POWDER SELF NODULIZE(3,1)\|PREHEATER TOP CYCLONE(3,1)\|QUALITATIVE PHASE(3,1)\|REACTED SAMPLE PHASE CONSTITUTION(3,1)\|REACTION ESCAPE(3,1)\|RED HE NE LASER(3,1)\|SAMPLE REACTION(3,1)\|SCRUBBING FLUE GAS(3,1)\|SESQUIHYDRATE(3,1)\|SILICA MOLE(3,1)\|SOLID PRECIPITATION(3,1)\|SOLUBLE SALT(3,1)\|STEEL CRUCIBLE(3,1)\|SULFUR CONTENT(3,1)\|ADSORPTION(2,1)\|AMORPHOUS SOLID CERAMICS(2,1)\|ANALYZING IMAGE(2,1)\|ANHYDROUS SODIUM CARBONATE(2,1)\|ANTIGORITE(2,1)\|AQUEOUS ACID(2,1)\|AUTOCLAVE(2,1)\|BASIC MAGNESIUM SILICATE(2,1)\|BRONZITE(2,1)\|BURNER(2,1)\|CALCINATION(2,1)\|CARBONATE PRODUCT(2,1)\|CHONDRODITE(2,1)\|CLOSED REACTOR(2,1)\|COMPLEX MAGNESIUM(2,1)\|CONVERSION YIELD(2,1)\|COUNTERCURRENT(2,1)\|DECAHYDRATE(2,1)\|DECARBONATION DEGREE(2,1)\|DECOMPOSITION(2,1)\|DIHYDRATE(2,1)\|DIOPSIDE(2,1)\|FAYALITE(2,1)\|FE2SI(2,1)\|FILTER CAKE DRYING(2,1)\|FILTERCAKE(2,1)\|FINE POWDER(2,1)\|GARNIERITE(2,1)\|GLASS REACTOR(2,1)\|GRANULE(2,1)\|HECTORITE(2,1)\|HOT WATER CIRCULATION(2,1)\|HOT ZONE(2,1)\|HUMITE(2,1)\|HYPERSTHENE(2,1)\|IDDINGSITE(2,1)\|INCOMING AIR(2,1)\|\|(CN103582611)\|MAGNESIUM 2 CARBONATE(100,17)\|MAGNESIUM 2 CARBONATE COMPOUND(100,9)\|MINERALIZING METHANEDIONE(100,2)\|MINERALIZE METHANEDIONE(100,1)\|FORMULA R2AN(37,1)\|FORMULA SIO2THE REACTION(37,1)\|METHANEDIONE(34,20)\|MAGNESIUM SILICATE(31,67)\|ALKALI MAGNESIUM SILICATE(28,25)\|ALKALI METAL CARBONATE(27,55)\|ALKALI METAL MAGNESIUM SILICATE(22,4)\|ALKALI METAL(21,76)\|ALKALI METAL BICARBONATE(19,8)\|BICARBONATE(18,6)\|MOLAR RATIO(13,6)\|PARTICULATE(10,6)\|COOLED DECARBONATED PELLET(9,2)\|GAS SCRUBBING(8,7)\|MAGNESIUM SILICATE ROCK(8,4)\|OLIVINE SAND(8,3)\|XH2O(8,2)\|LABORATORY FURNACE PLATINUM CRUCIBLE(8,1)\|METHANEDIONE MINERALIZATION(8,1)\|ALKALI METAL HYDROXIDE(7,3)\|DECARBONATED NODULE(7,1)\|LASER GRANULOMETRY(6,2)\|2SIO4OF GROUND OLIVINESAND(6,1)\|MAGNESIUM SILICATE1AMORPHOUS PRODUCT CARBONATION(6,1)\|MGCO SEPARATELY3AND(6,1)\|PERILLYL PYROXENE(6,1)\|PREHEATER CYCLONE COLUMN(6,1)\|UNREACTED OLIVESSTONE(6,1)\|SILICA RICH(5,3)\|DECARBONATION REACTION(5,2)\|EXCESS METHANEDIONE(5,2)\|SLURRY ADDITIVE(5,2)\|ABSORB METHANEDIONE(5,1)\|GASEOUS METHANEDIONE(5,1)\|OLIVINE STONE(5,1)\|PERCOLATED CAKE(5,1)\|PREHEATER TOWER(5,1)\|RELEASING METHANEDIONE(5,1)\|UNREACTED OLIVINE(5,1)\|ASBESTOS(4,4)\|CHRYSOTILE(4,3)\|NITRITE(4,3)\|COMBUSTION ZONE(4,2)\|GAS ABSORBER COLUMN(4,2)\|MAGNESIUM SILICATE MINERAL(4,2)\|ADDED2TO RETURN(4,1)\|ANHYDROUS MAGNESIUM SILICATE(4,1)\|CALCIUM FORSTERITE(4,1)\|FERMENTATION RESIDUE GAS(4,1)\|GASEOUS CO2UP(4,1)\|INORGANIC IMPURITY(4,1)\|LASER GRANULOMETER(4,1)\|MAGNESIUM REACTION(4,1)\|MAXIMUM THEORETICAL VALUE2AND(4,1)\|METHANEDIONE MIXING(4,1)\|METHANEDIONE VOLUME(4,1)\|MOVING GRATE COOLER(4,1)\|MOVING GRATE FURNACE(4,1)\|OLIVINE SAMPLE(4,1)\|PELLET BED(4,1)\|POROUS FRIT(4,1)\|PRECIPITATED SOLID PLUS SOLIDS1IN(4,1)\|ROCK ELEMENTAL ANALYSIS(4,1)\|SAMPLE DEAGGLOMERATION(4,1)\|SILICA MOLE(4,1)\|SLURRY ABSORPTION(4,1)\|STABLE NODULE(4,1)\|SUSPENSION PREHEATER(4,1)\|TRAVELING GRATE SPEED(4,1)\|UNREACTED MAGNESIUM SILICATE(4,1)\|AQUEOUS SOLUTION(3,4)\|ROTARY KILN(3,4)\|EXPERIMENT(3,3)\|STIRRER(3,3)\|ACTINOLITE(3,2)\|AMPHIBOLE(3,2)\|CHLORITE(3,2)\|ENSTATITE(3,2)\|FUEL COMBUSTION GAS(3,2)\|GAS STREAM(3,2)\|LOI DATA(3,2)\|MIXED POWDER(3,2)\|NET ENERGY CONSUMPTION(3,2)\|SIEVING(3,2)\|SODIUM CARBONATE HYDRATE POWDER(3,2)\|SODIUM CARBONATE POWDER(3,2)\|SODIUM CARBONATE SAMPLE(3,2)\|SULFITE(3,2)\|TREMOLITE(3,2)\|ULTRASOUND(3,2)\|ABOVETHE(3,1)\|ATMOSPHERE ABSOLUTE(3,1)\|BASIC MAGNESIUM ORTHOSILICATE(3,1)\|BIOMASS DERIVED FUEL(3,1)\|BLUE DIODE(3,1)\|BOUND ANALYSIS(3,1)\|CALCULATION MATRIX(3,1)\|CARBON DIOXIDERELEASING GAS(3,1)\|CO2CONTINUOUSLY(3,1)\|CRUSHED SAMPLE(3,1)\|EARTH CRUST DEEP LAYER(3,1)\|EFFLUENT GAS(3,1)\|GAS SCRUBBER(3,1)\|INCOMING COMBUSTION AIR PREHEATER(3,1)\|MAGNESIUM SILICATE HYDROXIDE(3,1)\|MANTLE2SIO COMPONENT(3,1)\|METHANEDIONE GAS ACTION(3,1)\|METHANEDIONE LEVEL(3,1)\|MGO SIO2THE MOLAR RATIO(3,1)\|NATURALLY OCCURRING MINERAL(3,1)\|OUTGOING HOT GAS(3,1)\|OUTGOING SOLID PARTICLE(3,1)\|PACKED BED(3,1)\|PASSINGTHE REACTION PRODUCT(3,1)\|POROUS BED(3,1)\|PREHEATER TOP CYCLONE(3,1)\|PREHEATER WALL(3,1)\|PROCESSES2AND(3,1)\|PROCESSES2THE EXHAUST GAS(3,1)\|QUANTITATIVE DETECTION(3,1)\|RED HE NE LASER(3,1)\|SAMPLE REACTION(3,1)\|SCRUBBING FLUE GAS(3,1)\|STEEL CRUCIBLE(3,1)\|STIRRED SUSPENSION(3,1)\|SULFUR CONTENT(3,1)\|ALKALI METAL OXIDE(2,5)\|AQUEOUS SUSPENSION(2,3)\|2CO3MOLAR(2,1)\|2SIO4MOLAR(2,1)\|AGITATION(2,1)\|AGITATOR SPEED(2,1)\|ALKALI METAL CARBONATESONE MOLE(2,1)\|ANHYDROUS SODIUM CARBONATE(2,1)\|ANTIGORITE(2,1)\|AUTOCLAVE(2,1)\|BRONZITE(2,1)\|BURNER(2,1)\|CALCINATION(2,1)\|CARBONATE RATIO(2,1)\|CARCINOGEN(2,1)\|CLOSED REACTOR(2,1)\|CO2THE LATTER VERTICAL ARROW(2,1)\|COMPLEX MAGNESIUM(2,1)\|DECAHYDRATE(2,1)\|DECARBONATION DEGREE(2,1)\|DECOMPOSITION(2,1)\|DIBUTONITE(2,1)\|DIHYDRATE(2,1)\|DIOPSIDE(2,1)\|DRY POWDER(2,1)\|ENERGY INTENSIVE(2,1)\|FAYALITE(2,1)\|FIBRIL(2,1)\|GAS2AND WATER(2,1)\|GLASS REACTOR(2,1)\|GRAM2CONSUMING(2,1)\|GROUND MAGNESIUM SILICATE(2,1)\|HEATING2SIO(2,1)\|HECTORITE(2,1)\|HELICOID(2,1)\|HOT WATER CIRCULATION(2,1)\|HOT ZONE(2,1)\|INCOMING SOLID(2,1)\|LEAVING ROOM(2,1)\|LIQUID FILTRATE(2,1)\|\|(CN103582611)\|MAGNESIUM 2 CARBONATE(100,19)\|MAGNESIUM 2 CARBONATE COMPOUND(100,11)\|MINERALIZE METHANEDIONE(100,3)\|MINERALIZING METHANEDIONE(61,2)\|MAGNESIUM SILICATE(35,81)\|METHANEDIONE(35,23)\|ALKALI MAGNESIUM SILICATE(31,30)\|MAGNESIUM SILICATE ROCK(23,6)\|ALKALI METAL CARBONATE(22,61)\|MAGNESIUM SILICATE COMPOUND(22,3)\|HEATED MIXTURE2O(22,1)\|PRECONCENTRATION(21,1)\|MAJOR TECHNICAL DIFFICULTY(20,1)\|SPECIALIZED EQUIPMENT(19,1)\|ALKALI METAL(18,87)\|ALKALI METAL BICARBONATE(18,10)\|MOVING GRATE(18,5)\|CARBONATION RATE(17,1)\|ELECTRICITY(17,1)\|FORMULA SIO2THE REACTION(17,1)\|GAS PURIFICATION(17,1)\|FORMULA R2AN(16,1)\|MAGNESIUM SILICATE MINERAL(15,3)\|ALKALI METAL MAGNESIUM SILICATE(14,4)\|MOLAR RATIO(12,7)\|BICARBONATE(12,6)\|CARBONATE SOURCE(12,1)\|SILICATE(11,3)\|GRANULE(10,1)\|PRESSURIZING(10,1)\|PELLET(9,15)\|COUNTERCURRENT HEAT EXCHANGE(9,4)\|SIO(9,4)\|GAS STREAM(9,3)\|MGO(8,8)\|PARTICULATE(8,6)\|FURNACE(8,4)\|COMBUSTION(8,2)\|BED(7,5)\|OLIVINE SAND(7,4)\|PRESSURE ELEVATION(7,3)\|COOLED DECARBONATED PELLET(7,2)\|FLUE GAS(6,7)\|GAS SCRUBBING(6,7)\|ATMOSPHERIC PRESSURE(6,5)\|STOICHIOMETRIC RATIO(6,3)\|UNREACTED OLIVINE(6,2)\|XH2O(6,2)\|LABORATORY FURNACE PLATINUM CRUCIBLE(6,1)\|METHANEDIONE MINERALIZATION(6,1)\|ALKALI METAL HYDROXIDE(5,3)\|LASER PARTICLE SIZER(5,2)\|DECARBONATED NODULE(5,1)\|MAGNESIUM SILICATE1AMORPHOUS PRODUCT CARBONATION(5,1)\|MGCO SEPARATELY3AND(5,1)\|PERILLYL PYROXENE(5,1)\|PREHEATER CYCLONE COLUMN(5,1)\|ENERGY EFFICIENCY(4,3)\|SILICA RICH(4,3)\|DECARBONATION REACTION(4,2)\|EXCESS METHANEDIONE(4,2)\|HEAT EXCHANGE(4,2)\|SLURRY ADDITIVE(4,2)\|ABSORB METHANEDIONE(4,1)\|GASEOUS METHANEDIONE(4,1)\|HEAT TRANSFER(4,1)\|OLIVINE STONE(4,1)\|PERCOLATED CAKE(4,1)\|PREHEATER TOWER(4,1)\|RELEASING METHANEDIONE(4,1)\|REACTION PRODUCT(3,8)\|ASBESTOS(3,4)\|CHRYSOTILE(3,3)\|NITRITE(3,3)\|COMBUSTION ZONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|ADDED2TO RETURN(3,1)\|ANHYDROUS MAGNESIUM SILICATE(3,1)\|AQUEOUS SLURRY(3,1)\|CALCIUM FORSTERITE(3,1)\|FERMENTATION RESIDUE GAS(3,1)\|GASEOUS CO2UP(3,1)\|INORGANIC IMPURITY(3,1)\|LASER GRANULOMETRY(3,1)\|MAGNESIUM REACTION(3,1)\|MAXIMUM THEORETICAL VALUE2AND(3,1)\|METAL OXIDE(3,1)\|METHANEDIONE GAS RELEASE(3,1)\|METHANEDIONE MIXING(3,1)\|METHANEDIONE VOLUME(3,1)\|MOVING GRATE COOLER(3,1)\|MOVING GRATE FURNACE(3,1)\|OLIVINE SAMPLE(3,1)\|PELLET BED(3,1)\|POROUS FRIT(3,1)\|PRECIPITATED SOLID PLUS SOLIDS1IN(3,1)\|PREHEAT KILN INCOMING COMBUSTION AIR(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SILICA MOLE(3,1)\|SLURRY ABSORPTION(3,1)\|STABLE NODULE(3,1)\|SUSPENSION PREHEATER(3,1)\|TRAVELING GRATE SPEED(3,1)\|UNREACTED MAGNESIUM SILICATE(3,1)\|CARBON DIOXIDE(2,14)\|AQUEOUS SOLUTION(2,4)\|ROTARY KILN(2,4)\|AQUEOUS SUSPENSION(2,3)\|EXPERIMENT(2,3)\|STIRRER(2,3)\|ACTINOLITE(2,2)\|AMPHIBOLE(2,2)\|ENSTATITE(2,2)\|FUEL COMBUSTION GAS(2,2)\|LOI DATA(2,2)\|MIXED POWDER(2,2)\|NET ENERGY CONSUMPTION(2,2)\|SIEVING(2,2)\|SODIUM CARBONATE HYDRATE POWDER(2,2)\|SODIUM CARBONATE POWDER(2,2)\|SODIUM CARBONATE SAMPLE(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|ATMOSPHERE ABSOLUTE(2,1)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|BOUND ANALYSIS(2,1)\|CALCULATION MATRIX(2,1)\|CO2CONTINUOUSLY(2,1)\|CRUSHED SAMPLE(2,1)\|EARTH CRUSTCHLORITE DEEP LAYER(2,1)\|EFFLUENT GAS(2,1)\|GAS SCRUBBER(2,1)\|MAGNESIUM SILICATE HYDROXIDE(2,1)\|MANTLE2SIO COMPONENT(2,1)\|METHANEDIONE GAS ACTION(2,1)\|METHANEDIONE LEVEL(2,1)\|MGO SIO2THE MOLAR RATIO(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|OUTGOING HOT GAS(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED(2,1)\|POROUS BED(2,1)\|PREHEATER TOP CYCLONE(2,1)\|PREHEATER WALL(2,1)\|PROCESSES2AND(2,1)\|PROCESSES2THE EXHAUST GAS(2,1)\|QUANTITATIVE DETECTION(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|STIRRED SUSPENSION(2,1)\|SULFUR CONTENT(2,1)\|2CO3MOLAR(1,1)\|2SIO4MOLAR(1,1)\|2SIO4THE(1,1)\|AGITATION(1,1)\|AGITATOR SPEED(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AUTOCLAVE(1,1)\|BASETHE(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CARBONATE RATIO(1,1)\|CARCINOGEN(1,1)\|CLOSED REACTOR(1,1)\|CO2THE LATTER VERTICAL ARROW(1,1)\|COMPLEX MAGNESIUM(1,1)\|COMPOUNDS2O(1,1)\|COUNTERCURRENT(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIBUTONITE(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|DRY POWDER(1,1)\|ENERGY INTENSIVE(1,1)\|FAYALITE(1,1)\|FIBRIL(1,1)\|FINENESS(1,1)\|GAS2AND WATER(1,1)\|GLASS REACTOR(1,1)\|GRAM2CONSUMING(1,1)\|\|(KR10-2014-0045459)\|MAGNESIUM CARBONATE(100,19)\|MAGNESIUM CARBONATE COMPOUND(100,11)\|MINERALIZING CARBON DIOXIDE(100,2)\|ASBESTOS MICROFIBER(95,1)\|PROPORTION CARBONATION(86,1)\|MINERALIZE CARBON DIOXIDE(73,4)\|MICROPOLISHED MAGNESIUM SILICATE(70,1)\|MAGNESIUM SILICATE(68,80)\|ROCK MAGNESIUM SILICATE(56,1)\|PRECONCENTRATION(51,1)\|ALKALI METAL BICARBONATE(50,15)\|HOT EFFLUENT GAS(47,1)\|ALKALI METAL CARBONATE(45,64)\|GAS PURIFICATION(45,1)\|TECHNICAL DIFFICULTY(45,1)\|HOT EFFLUENT SOLID(42,1)\|ALKALI METAL(40,124)\|ALKALI METAL MAGNESIUM SILICATE(40,35)\|MAGNESIUM SILICATE ROCK(40,4)\|HYDRATING WATER(40,1)\|PRESSURIZING(39,1)\|MAGNESIUM SILICATE MINERAL(36,4)\|INCOMING SOLID(34,1)\|COMBUSTION(33,2)\|CARBON DIOXIDE(32,34)\|ANHYDROUS ALKALI METAL CARBONATE(32,1)\|BICARBONATE(30,7)\|MAGNESIUM SILICATE REACTION(30,5)\|MOLE(29,40)\|INCOMING COMBUSTION AIR(29,1)\|ALKALI METAL SILICATE(28,1)\|COUNTERCURRENT HEAT EXCHANGE(26,3)\|NET ENERGY CONSUMPTION(26,2)\|HEALTH(26,1)\|FURNACE(25,4)\|ANHYDROUS ALKALI METAL(25,1)\|GAS STREAM(23,3)\|EARTH OLIVINE(19,4)\|PRESSURE ELEVATION(19,3)\|MOLAR RATIO(18,4)\|ENERGY CONSUMPTION(18,1)\|FLUE GAS(17,7)\|PREHEATER CYCLONE TOWER(17,1)\|CARBON DIOXIDE GAS(16,4)\|ABRADED OLIVINE SAND(15,1)\|MAGNESIUM SILICATE CARBONATION(15,1)\|ALKALI METAL HYDROXIDE(13,3)\|EXPERIMENTAL FURNACE(13,3)\|PREDOMINANTLY AMORPHOUS PRODUCT(13,3)\|EARTH MANTLE(13,2)\|EARTH PERCEPTION(13,2)\|PLATINUM CRUCIBLE(13,2)\|CLEANING GAS(12,7)\|SILICON DIOXIDE(12,4)\|COOLED DECARBONATED PALLET(12,1)\|DECARBONATED CLUMP(12,1)\|GALLATE SOPHILITE(12,1)\|MITIGATION WHEEHMITE(12,1)\|PALLET PACKED BED(12,1)\|DISRUPTION(11,6)\|PARTICULATE(11,6)\|ANHYDROUS MAGNESIUM SILICATE(11,2)\|DECARBONATION REACTION(11,2)\|MOVING GRATE FURNACE(11,2)\|PRESSURE REACTOR(11,2)\|HEAT EXCHANGE(10,3)\|HELICOIDAL TEFLON(10,1)\|KAOLIN OLIVINE(10,1)\|PREHEATER TOWER(10,1)\|UNREACTED OLIVINE(10,1)\|ATMOSPHERIC PRESSURE(9,5)\|CRYSTALIZATION SPECIALIZATION(9,1)\|LASER GRANULOMETER(9,1)\|LASER GRANULOMETRY(9,1)\|MAX CO2(9,1)\|PALLET BATCH(9,1)\|PALLET BED(9,1)\|SAMPLE DEAGGLOMERATION(9,1)\|SHIELD STABILIZATION(9,1)\|SUSPENSION PREHEATER(9,1)\|REACTION PRODUCT(8,8)\|ATINITE(8,3)\|FUEL COMBUSTION GAS(8,3)\|HYDROMAGNESITE(8,3)\|NITRITE(8,3)\|COMBUSTION ZONE(8,2)\|GAS ABSORBER COLUMN(8,2)\|AQUEOUS SOLUTION(7,4)\|ADHEREND FORMATION(7,1)\|BEEN CONSIDERED CARCINOGEN(7,1)\|CO2 ATM(7,1)\|COMPUTATIONAL MATRIX(7,1)\|FERMENTATION RESIDUE GAS(7,1)\|INDUSTRIAL APPLICATION(7,1)\|INORGANIC IMPURITY(7,1)\|IRON OLIVINE(7,1)\|MAGNESIUM SILICATE HYDRATE(7,1)\|OLIVINE SAMPLE(7,1)\|PACKED BED COLUMN(7,1)\|SLURRY ADDITIVE(7,1)\|STABLE NODULE(7,1)\|UNREACTED MAGNESIUM SILICATE(7,1)\|WARM WOOL(7,1)\|HOT GAS(6,4)\|ROTARY KILN(6,4)\|MG2SI(6,3)\|ACTINOLITE(6,2)\|CHLORITE(6,2)\|INTERRUPTION(6,2)\|MEASURED LOI DATA(6,2)\|MIXED POWDER(6,2)\|SIEVING(6,2)\|SODIUM CARBONATE HYDRATE POWDER(6,2)\|SODIUM CARBONATE SAMPLE(6,2)\|SULFITE(6,2)\|ULTRASOUND(6,2)\|ALWAYS PURE SILICATE(6,1)\|BASIC MAGNESIUM NONANOATE(6,1)\|BLUE DIODE(6,1)\|DRIED FILTER DEBRIS(6,1)\|EFFLUENT GAS(6,1)\|EFFLUENT SOLID PARTICLE(6,1)\|EXAMPLE2SI(6,1)\|FE2SI04PAUL(6,1)\|GAS SCRUBBER(6,1)\|GAS SCRUBBING(6,1)\|HEATING JACKET(6,1)\|HOT NODULE HEAT(6,1)\|INCOMING COMBUSTION AIR PREHEATER(6,1)\|JOINED FILTRATE(6,1)\|KILN OUTLET GAS(6,1)\|MINERALIZATION(6,1)\|PALLET MECHANICAL INTEGRITY(6,1)\|PALLETIZATION(6,1)\|POLYDISPERSITY(6,1)\|POROUS BED(6,1)\|POTASSIUM CARBONATE HYDRATE(6,1)\|PREHEATER TOP CYCLONE(6,1)\|QUALITATIVE PHASE(6,1)\|RED HE NE LASER(6,1)\|SAMPLE MEASURED IGNITION(6,1)\|SAMPLE REACTION(6,1)\|SILICINICKELITE(6,1)\|SOLID PRECIPITATION(6,1)\|SOLUBLE SALT(6,1)\|STEEL CRUCIBLE(6,1)\|STOICHIOMETRY RATIO(6,1)\|SUBPREFERRED STOICHIOMETRIC RATIO(6,1)\|SULFUR CONTENT(6,1)\|AQUEOUS SUSPENSION(5,3)\|MAJOR SOLID PRODUCT(5,3)\|MGCO3(5,3)\|UNITY(5,3)\|PELLET(5,2)\|ABSORB CARBON DIOXIDE(4,1)\|ACID DILUTION(4,1)\|ADDRESSING(4,1)\|ADSORPTION(4,1)\|ANHYDRIDE(4,1)\|ANHYDROUS SODIUM CARBONATE(4,1)\|ANTHOPHYLLITE(4,1)\|ASBESTOS(4,1)\|AUTOCLAVE(4,1)\|BASIC MAGNESIUM SILICATE(4,1)\|BIOMASS(4,1)\|CALCINATION(4,1)\|CARBON DIOXIDE CONVERSION(4,1)\|CARBONATE RATIO(4,1)\|CASE2SI(4,1)\|CHONDRODITE(4,1)\|CLEANING FLUE GAS(4,1)\|CLOSED REACTOR(4,1)\|COMBINED CO2(4,1)\|COMBUSTOR(4,1)\|COUNTERCURRENT(4,1)\|DECAHYDRATE(4,1)\|DECARBONATION DEGREE(4,1)\|DECOMPOSITION(4,1)\|DEEP LAYER(4,1)\|DISINTEGRATION(4,1)\|DRY POWDER(4,1)\|ENERGY INTENSIVE(4,1)\|FINAL MELT(4,1)\|FINAL POWDER(4,1)\|FINE POWDER(4,1)\|GALLSTONE(4,1)\|GASEOUS CARBON DIOXIDE(4,1)\|GLASS REACTOR(4,1)\|GRATING(4,1)\|HECTORITE(4,1)\|HEMIHYDRATE(4,1)\|HEURITE(4,1)\|HOT WATER CIRCULATION(4,1)\|HOT ZONE(4,1)\|HYDRATION WATER(4,1)\|IDINSITE(4,1)\|INCLUSIVE SHAPE(4,1)\|\|(CA2838035)\|MAGNESIUM 2 CARBONATE(100,20)\|MAGNESIUM 2 CARBONATE COMPOUND(100,11)\|METHANEDIONE MINERALIZATION(100,6)\|METHANEDIONE CAPTURE(30,1)\|MAGNESIUM SILICATE(27,82)\|METHANEDIONE(27,23)\|MAGNESIUM SILICATE ROCK(20,6)\|PRECONCENTRATION(18,1)\|ALKALI METAL MAGNESIUM SILICATE(17,37)\|MAJOR TECHNICAL DIFFICULTY(17,1)\|OUTGOING HOT GAS(17,1)\|ALKALI METAL CARBONATE(16,60)\|MOVING GRATE FURNACE(16,2)\|SPECIALIZED EQUIPMENT(16,1)\|OUTGOING HOT SOLID(15,1)\|ALKALI METAL(14,119)\|GAS PURIFICATION(14,1)\|GROUND MAGNESIUM SILICATE(14,1)\|ALKALI METAL BICARBONATE(13,10)\|FURNACE(13,4)\|MAGNESIUM SILICATE MINERAL(13,3)\|INCOMING SOLID(13,1)\|PRESSURIZING(13,1)\|METHANEDIONE GAS(12,4)\|BICARBONATE(11,5)\|CARBONATION(11,2)\|MOVING GRATE(10,5)\|NET ENERGY CONSUMPTION(10,2)\|INCOMING COMBUSTION AIR(10,1)\|COUNTERCURRENT HEAT EXCHANGE(9,3)\|PELLET(8,14)\|COOLED DECARBONATED PELLET(8,4)\|GAS STREAM(8,3)\|XH2O(7,1)\|MOLAR RATIO(6,9)\|FLUE GAS(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|PRESSURE ELEVATION(6,3)\|COMBUSTION(6,2)\|PREHEATER CYCLONE TOWER(6,1)\|GAS SCRUBBING(5,7)\|UNREACTED OLIVINE(5,2)\|HYDROMAGNESITE(4,6)\|AMORPHOUS PRODUCT(4,4)\|ALKALI METAL HYDROXIDE(4,3)\|LAB FURNACE(4,3)\|EARTH CRUST(4,2)\|LASER GRANULOMETRY(4,2)\|PLATINUM CRUCIBLE(4,2)\|ASBESTOS FIBRILLAR(4,1)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|DECARBONATED NODULE(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|OBSCURATION STABILIZATION(4,1)\|ATMOSPHERIC PRESSURE(3,5)\|FORSTERITE(3,5)\|PARTICULATE(3,5)\|FILTER CAKE DRYING(3,4)\|ANHYDROUS PRODUCT(3,3)\|ENERGY EFFICIENCY(3,3)\|ANHYDROUS MAGNESIUM SILICATE(3,2)\|BURNING ZONE(3,2)\|DECARBONATION REACTION(3,2)\|EXCESS METHANEDIONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|PRESSURE REACTOR(3,2)\|SLURRY ADDITIVE(3,2)\|ABSORB METHANEDIONE(3,1)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GASEOUS METHANEDIONE(3,1)\|GROUND OLIVINE MIX(3,1)\|HEAT TRANSFER(3,1)\|HELICOIDAL TEFLON(3,1)\|HYDRO MAGNESITE(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|PREHEATER TOWER(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SUSPENSION PREHEATER(3,1)\|REACTION PRODUCT(2,7)\|EXPERIMENT(2,5)\|AQUEOUS SOLUTION(2,4)\|HOT GAS(2,4)\|ROTARY KILN(2,4)\|FUEL COMBUSTION GAS(2,3)\|MG2SIO(2,3)\|NITRITE(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|MEASURED LOI DATA(2,2)\|MG094FE(2,2)\|MGO SI(2,2)\|MIXED POWDER(2,2)\|PYROXENE(2,2)\|SIEVING(2,2)\|SODIUM CARBONATE POWDER(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CRUSHED SAMPLE(2,1)\|EARTH MANTLE COMPONENT(2,1)\|ESTIMATED MG(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE NESS(2,1)\|FINE SAND GRANULOMETRY(2,1)\|FORMULA SI(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|QUALITATIVE PHASE(2,1)\|QUANTITATIVE DETECTION(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SELFNODULIZATION(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|STEEL CRUCIBLE(2,1)\|SULFUR CONTENT(2,1)\|SUSPENSION AGITATION(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|AQUEOUS SUSPENSION(1,3)\|CO2(1,3)\|STOICHIOMETRIC RATIO(1,3)\|ADSORPTION(1,1)\|AMORPHOUS SOLID RICH(1,1)\|ANALYZING IMAGE(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CARBONATE PRODUCT(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|CONVERSION YIELD(1,1)\|COUNTERCURRENT(1,1)\|CRYSTALLINE PHASE(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|ENERGY INTENSIVE(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FILTERCAKE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GLASS REACTOR(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT WATER CIRCULATION(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|	(EP2718230)\|1. A process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|2. A process according to claim 1 in which the carbon dioxide is in the free form in a gas comprising carbon dioxide.\|3. A process according to claim 1 in which the carbon dioxide is in the form of an alkali metal carbonate or bicarbonate formed by contacting a gas comprising carbon dioxide with an alkali metal hydroxide or an alkali metal carbonate.\|4. A process according to any one of the preceding claims in which the alkali metal magnesium silicate is prepared by the reaction of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate.\|5. A process according to any one of the preceding claims in which the alkali metal magnesium silicate is prepared by the reaction, at a temperature from 500 to 1100°C, of an alkali metal carbonate compound which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide of the formula SiO2, being from 2:1 to 1:2, which reaction produces an alkali metal magnesium silicate.\|6. A process according to claim 5 in which the reaction is effected at a temperature of 800 to 950°C.\|7. A process according to claim 5 or 6 in which the magnesium silicate is of the general formula m(MgO)-SiO2-xH2O wherein m is from 0.5 to 3 and x is from zero to 2.\|8. A process according to any one of claims 5 to 7 in which the reaction of the alkali metal carbonate compound and the magnesium silicate is effected in the solid state.\|9. A process according to any one of the preceding claims in which the alkali metal magnesium silicate is in shaped or particulate form.	(EP2718230)\|[0001] This invention relates to a process for the mineralization of carbon dioxide from, for example, a gas stream such as the flue gases from an industrial combustion process. The process uses as starting material an alkali metal magnesium silicate and produces magnesium carbonate compounds and silica.\|[0002] In WO 2010/097451 magnesium-comprising silicate hydroxide particles are heated alone to activate the particles, which are then ground to a smaller size and contacted with an aqueous medium (which preferably contains a dissolved bicarbonate salt) and carbon dioxide under low temperature conditions. The solution and small activated particles are then contacted with carbon dioxide at elevated temperatures (preferably at least 140°C, and therefore under pressure to avoid the water simply boiling off).\|[0003] US2009/0202410 similarly discloses contacting an aqueous alkali metal carbonate solution with carbon dioxide to obtain a bicarbonate solution, which is then contacted with a waste material. The mineral may contain, inter alia, a magnesium-containing silicate mineral.\|[0004] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into magnesium silicate hydrate minerals such as serpentine or chlorite (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10)(OH)2).\|[0005] Magnesium silicate rocks constitute an excellent source of basic magnesium which should in theory readily be converted into stable magnesium carbonate compounds by the action of carbon dioxide gas under normal atmospheric conditions. However, in practice, the weathering and carbonation of natural magnesium silicate minerals at the Earth's surface occurs only very slowly. Thus, while the use of magnesium silicates as a source of basic magnesium for the mineralization of carbon dioxide has been proposed as a means to combat the current trend towards increasing carbon dioxide levels in the atmosphere, processes to achieve such mineralization have heretofore been excessively energy-intensive, as well as excessively expensive to set up and operate, and, and thus have not been commercialized. One of the major technical difficulties which renders such processes so expensive to set up and operate is the need to use elevated pressures and temperatures in order to achieve a sufficiently high rate (for industrial purposes) of carbonation of magnesium silicate minerals. Typically, the carbon dioxide gas must first be purified and then compressed to pressures in excess of 70 atmospheres, and then contacted with finely-ground magnesium silicates in a pressure reactor at temperatures of 120-200°C. This requires specialized equipment which is expensive to build and maintain, as well as large amounts of electric power to operate the gas purification and pressurization process as well as to finely grind the magnesium silicate rocks.\|[0006] Although the common magnesium silicate minerals listed above tend to be very "unreactive," (e.g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a "carbonate fusion", is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analysed by standard chemical techniques, thus allowing for total elemental analysis of the rock. The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0007] US 5,085,838A describes a process for reacting an asbestiform material, which may be a magnesium-containing mineral, with an alkaline flux, which may be an alkali metal carbonate, into an environmentally safe glassy material by heating to about 750°C to 1000°C. An X-ray diffraction spectrum attributes one peak to an alkali metal magnesium silicate. The glassy material produced is described as a safe, non-toxic waste, which can be disposed of, or used as a process feed-stock for producing various glassy products.\|[0008] JP2007/146094 describes the use of a water-swelling clay, named as sodium-magnesium silicate, in a detergent composition suitable for cleaning skin. The clay, which is a known material, is not a true alkali metal magnesium silicate, contains lithium as part of its structure and is known by a number of synonyms including lithium magnesium sodium salt, synthetic magnesium lithium silicate and lithium magnesium sodium silicate.\|[0009] The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step.\|[0010] The present invention accordingly provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|[0011] The alkali metal is preferably potassium or, more preferably, sodium.\|[0012] The process is preferably effected at a temperature of 25 to 100°C, more preferably 35 to 80°C. The carbon dioxide may be in the free form in a gas comprising carbon dioxide.\|[0013] The process of the invention can be used to remove carbon dioxide from a gas at a reduced or elevated pressure or, for example, at about atmospheric pressure. The process of the invention may be carried out on a carbon dioxide-containing gas at an absolute pressure generally from 0.5 to 100 bar, preferably from 1 to 20 bar, most preferably at about 1 bar.\|[0014] The gas to be treated may contain from 0.01% to 100% carbon dioxide by volume, preferably from 0.1% to 50%, more preferably from 1% to 40%, and most preferably from 4% to 30%. The gas stream may be a flue gas from an industrial combustion process.\|[0015] The carbon dioxide may also be in the form of an alkali metal carbonate or bicarbonate formed by contacting a gas comprising carbon dioxide with an alkali metal hydroxide or an alkali metal carbonate. The alkali metal carbonate or bicarbonate is preferably produced in the form of an aqueous solution, prepared by reaction between an aqueous solution of an alkali metal hydroxide or carbonate and gaseous carbon dioxide.\|[0016] The alkali metal magnesium silicate is preferably in particulate form, for example a powder, preferably having a Blaine specific surface area of 100 to 800m2/kg, more preferably 200 to 650m2/kg.\|[0017] The process according to the invention is preferably effected with a product comprising alkali metal magnesium silicate. The alkali metal magnesium silicate is preferably prepared by the reaction of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate, or a mixture thereof, with a magnesium silicate. The alkali metal carbonate compound used preferably comprises alkali metal carbonate produced by contacting a gas comprising carbon dioxide with an alkali metal magnesium silicate generally in the presence of water, the alkali metal magnesium silicate being converted into a solution of an alkali metal carbonate plus solid residues comprising magnesium carbonates and a largely amorphous product rich in silica and containing some magnesium by reaction with the carbon dioxide, and the alkali metal carbonate solution being separated and concentrated prior to reaction with the magnesium silicate.\|[0018] The invention also provides a process for the preparation of a product comprising an alkali metal magnesium silicate compound (which compound is preferably of composition R2O•MgO•SiO2, (in which R represents an alkali metal),which process comprises the reaction, at a temperature from 500 to 1100°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 2:1 to 1:2, which reaction produces the product comprising an alkali metal magnesium silicate.\|[0019] The product produced by this process may be in shaped or particulate form.\|[0020] The product may be used to provide a slurry, generally aqueous, comprising an alkali metal magnesium silicate produced by this process.\|[0021] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate expressed as silicon dioxide is preferably from 2:1 to 1:2, more preferably from 3:2 to 2:3, for example 4:3 to 3:4. The ratio is most preferably about 1.\|[0022] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used to prepare the alkali metal magnesium silicate.\|[0023] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0024] The magnesium silicate used in the preparation of the alkali metal magnesium silicate is generally a mineral silicate, for example a rock comprising a high concentration, preferably 20% or more, more preferably 50% or more, of a magnesium silicate of the general formula:\| m(MgO)•t(MeO)•SiO2•xH2O\|wherein Me represents a metal or metals other than magnesium, (such as, for example, calcium and/or iron); m is from 0.5 to 3, preferably from1 to 3, t is less than or equal to 1, and x is from zero to 2.\|[0025] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc iddingsite and hectorite. These minerals may contain substantial quantities of calcium, iron and alkali metals in addition to magnesium and silicon. Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, anthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens. The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0026] The mineral silicate used to prepare the alkali metal magnesium silicate is preferably a basic magnesium silicate. The MgO/SiO2 molar ratio is preferably from 1 to 3. The CaO/SiO2 molar ratio is preferably ≤0.5. The FeO/SiO2 molar ratio is preferably ≤0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≤0.2.\|[0027] The alkali metal carbonate compound used in the preparation of the alkali metal magnesium silicate may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2•2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g. chlorides, sulfates, sulfites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates, nitrites or hydroxides) are present which, at the temperature used to prepare the alkali metal magnesium silicate, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0028] The process used to prepare the alkali metal magnesium silicate is preferably effected at a temperature from 600 to 1000°C, for example 700 to 950°C, more preferably from 800 to 950°C. Heating is generally effected for a few minutes to a few hours, for example from 5 minutes to 24 hours, preferably from 10 minutes to 4 hours.\|[0029] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is slightly below its melting point.\|[0030] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as "R2O" in which R represents an alkali metal) present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt. = 140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt. = 106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0031] The magnesium silicate and alkali metal carbonate compound used to prepare the alkali metal magnesium silicate are preferably in particulate form or in shaped form, e.g. as pellets. Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the preparation of the alkali metal magnesium silicate will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of fine sand (grain size 0.06 to 0.2mm) or, if necessary, ground to a fine powder (grain sizes below 0.06mm). Grain sizes greater than 0.06mm are generally determined by sieving. Grain sizes lower than 0.06mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0032] In one embodiment the process to prepare the alkali metal magnesium silicate is conducted in a moving grate furnace.\|[0033] For example a mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in Figure 1 of the accompanying drawings.\|[0034] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0035] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone ("burning zone") just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate:\| (1) Mg2SiO4 + R2CO3 ⇒ product comprising R2MgSiO4 + CO2↑\|in which R is as hereinbefore defined: R preferably represents sodium.\|[0036] The vertical arrow ↑ after CO2 indicates that the carbon dioxide gas produced by this reaction escapes from the bed and exits with the rest of the exhaust gases. The idealized reaction depicted in equation (1) illustrates the production of a product comprising an alkali metal magnesium silicate by direct reaction of a stoichiometric mixture of forsterite and an alkali metal carbonate. This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 2.6 kJ (i.e. about 0.6 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, the net energy consumption for the overall process will be significant. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0037] In a further embodiment, the preparation of the alkali metal magnesium silicate is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln in a decarbonation step which produces carbon dioxide.\|[0038] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0039] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 40% of the total solids volume. In order to achieve this, it may sometimes be necessary to reduce the R2O/SiO2 ratio of the initial pellet composition to a value substantially below the preferred stoichiometric ratio of 1. The degree of reaction of the magnesium silicate during the process will then also be less than 100% but the effect of this can potentially be mitigated by separating the unreacted magnesium silicate from the reaction products and recycling it together with additional magnesium silicate starting material in the production of a fresh batch of pellets.\|[0040] According to a further feature of the invention the preparation of the alkali metal magnesium silicate is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The R2O/SiO2 ratio may be less than 1 if necessary in order to form substantially stable nodules. The nodules are decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0041] The cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate are then used in a gas scrubbing system designed to remove carbon dioxide from a gas at a reduced or elevated pressure or, for example, at about atmospheric pressure.\|[0042] In one embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are ground in water to make an aqueous suspension or slurry which can be directly injected into a conventional gas scrubbing system, such as a spray tower.\|[0043] In another embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are packed into a vertical column to form a packed bed of pellets through which a gas can be passed from bottom to top, while at the same time a suitably-controlled spray of water is added at the top of the column to ensure that the pellets remain wet. This constitutes a counter-current packed-bed gas absorber column. The flow of water leaving the bottom of this column is collected and treated as described later in more detail. The pellets or nodules used to form this type of packed bed column may be pre-selected for their dimensions and mechanical strength.\|[0044] In both of the above embodiments, the reactions occurring in the gas scrubbing system or gas absorber column are as follows:\| (2) R2MgSiO4(S) + (1+p)CO2(g) + water ⇒ (MgO)•p(CO2)•q(H2O)(s) + solid1 + R2CO3 (aq.)\|Where:\| The terms (s), (g) and (aq.) indicate solid, gas, and aqueous solution, respectively,\| p is > 0 and less than or equal to 1. Preferably, p is greater than or equal to 0.5\| q may be zero but can also take values as high as 3 in some cases.\|[0045] The principal solid products are:\| a magnesium carbonate compound, (MgO)•p(CO2)•q(H2O), which may contain more than one chemical compound, and in which a significant fraction of the carbon dioxide captured from the gas stream is contained in a stable solid form; and\| solid1 which is a largely amorphous solid rich in silica and containing some magnesium.\|[0046] These two principal solid products will generally be intimately mixed.\|[0047] Other minor solid products that may also be present include iron oxides, hydroxides or carbonates, as well as calcium carbonates.\|[0048] The alkali metal carbonate solution resulting from the gas scrubbing process will, if reaction (2) goes to completion, contain all of the alkali metal ions present in the original solid product. It is therefore desirable to separate this alkali metal carbonate solution and extract the alkali metal carbonates in solid form for re-use in the high temperature process according to reaction (1). In principle, this can be done most effectively by a combination of evaporation and crystallization processes, making use of the waste heat available both from the decarbonation reaction (1) and also from the flue gas scrubbing system, (noting that reactions (2) and (3) are both highly exothermic and thus that the gas scrubbing system itself is likely to operate at a higher temperature than the temperature of the flue gases being treated by it, thus producing a hot solution of alkali metal carbonate).\|[0049] Some other salts may be present in the alkali metal carbonate solution due to impurities in the magnesium silicate rocks or the flue gases. The most common impurities are likely to be alkali metal sulfates, sulfites, nitrates and nitrites. Under certain circumstances it may be necessary to separate these salts from the recycled alkali metal carbonate by specialized crystallization and washing procedures.\|[0050] In yet another embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are crushed, and if necessary ground, to a suitable median particle size. They are then contacted with a solution comprising an alkali metal bicarbonate in, for example, a tank, preferably with some mechanical stirring. The alkali metal bicarbonate solution may originate from a gas scrubbing system designed to capture carbon dioxide from a gas at, for example, atmospheric pressure. Typical reactions between the alkali-metal bicarbonate solution and the solids in this case is shown by the following equations:\| (3) R2MgSiO4(s) + 2(1+p)RHCO3(aq.) + water ⇒ (MgO)•p(CO2)•q(H2O)(s) + solid1 + (2+p)R2CO3 (aq.)\|[0051] The solid1 is as described above.\|[0052] The alkali metal bicarbonate solution (RHCO3(aq.)) used in reaction (3) may be formed by the reaction of the alkali metal carbonate solution (R2CO3(aq.)) produced in reaction (3) with carbon dioxide and water as shown in reaction (4):\| (4) R2CO3 (aq.) + CO2(g) + water ⇒ 2RHCO3(aq.)\|[0053] This reaction can be conducted in a separate gas scrubbing system, thus participating in a closed-loop alkali-carbonate/bicarbonate gas scrubbing system.\|[0054] The reactions described above are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid magnesium carbonate compounds. The magnesium carbonate solid produced may comprise either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or complex magnesium hydroxy-carbonate hydrates, such as artinite (Mg(OH)2•MgCO3•3H2O), or hydromagnesite, (Mg(OH)2•4MgCO3•4H2O), depending on the conditions. All of these precipitated solids, plus the solid1, will in many cases be finer than the unreacted starting material (Mg2SiO4 in this example), and so could be separated from it by sedimentation and then separated from the alkali metal carbonate which remains in solution by filtration. The unreacted starting material (Mg2SiO4 in this case) thus separated can be recycled to the beginning of the process. The alkali metal carbonate solution can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and also recycled to the start of the process. The mixture of magnesium carbonates and largely amorphous product rich in silica and containing some magnesium produced by these reactions is one of the final products of the overall process (and constitutes a feature of the invention) and can be separated for disposal or for use in other processes.\|[0055] One overall object of the process of the invention is to use common magnesium silicate rocks to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable magnesium carbonate compound.\|[0056] An example of a process of the invention which seeks to maximise capture of CO2 from exhaust gases from other industrial processes and to convert it substantially completely into solid magnesium carbonates in an energy-efficient way, not requiring any high-pressure reactors or autoclaves of the type usually required for direct carbonation of magnesium silicates, is shown in Figure 2 (in which solid1 is a largely amorphous product rich in silica and containing some magnesium).\|[0057] Raw materials are prepared to form a mixture of one part of a magnesium silicate (mMgO.SiO2.xH2O) plus another part being a combination of one or more alkali metal carbonate compounds for which the combined composition is represented by the formula (R2O.nCO2.yH2O); the mixture is heated by fuel combustion gases from a burner supplied with fuel and air; the heated mixture reacts to form a product comprising an alkali metal magnesium silicate (R2O.MgO.SiO2) and to release carbon dioxide which mixes with the fuel combustion gases to form exhaust gases with excess carbon dioxide; liquid water is added to the reaction product and the product is wet ground to form a slurry; the slurry is contacted in a gas scrubber with the exhaust gases with excess carbon dioxide produced earlier and with CO2-containing exhaust gases from other processes to absorb carbon dioxide and to produce a slurry comprising magnesium carbonate and silicon dioxide; the slurry is filtered to produce a filtercake comprising magnesium carbonate and a largely amorphous product rich in silica and containing some magnesium; the filter-cake is dried to produce a mixed solid product which is dried; the filtrate comprising alkali metal carbonate compound in solution is dried or crystallized to produce solid alkali metal carbonate compound which is recycled for use as starting material.\|[0058] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0059] The term "pellets" as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0060] Particle size and size distribution when measured by laser granulometry for particle sizes less than about 100µm are measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He-Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.The apparatus is checked before each working session by means of a standard sample (Sifraco C10 silica) for which the particle size distribution is known.\|[0061] Measurements are performed with the following parameters: pump speed 2300rpm and stirrer speed 800rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30s (for possible air bubbles to clear), a measurement is carried out for 15s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0062] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0063] Particle sizes and particle size distributions for particle sizes greater than about 100µm are measured by sieving.\|[0064] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R, m, t, x, p, n, z and y are as initially defined.\|[0065] The following non-limiting Examples illustrate embodiments of the invention.\|EXAMPLE 1\|[0066] Ground olivine sand of composition (Mg0.94Fe0.06)2SiO4 was mixed with a sodium carbonate hydrate powder in a 14:11 mass ratio. 25g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800°C over 2 hours, maintained at 800°C for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table 1:\|Table 1SampleLoss on IgnitionSodium carbonate powder14.97 %Ground olivine sand0.22 %14:11 mix of ground olivine sand + sodium carbonate powder16.69 %\|[0067] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by X-ray diffraction. The reaction products observed by this technique included Na2MgSiO4 and Fe2O3 together with some unreacted olivine and sodium carbonate.\|EXAMPLE 2\|[0068] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. (The molar ratio of this mixture is close to 1). The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900°C. The sample was air-quenched after 1h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851 °C). The measured loss on ignition of all of the samples is presented in the following Table 2 :\|Table 2SampleLoss on IgnitionSodium carbonate14.96 %Olivine0.04 %Olivine + Sodium carbonate23.02 %\|[0069] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by X-ray diffraction and the main phases detected included Na2MgSiO4, together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data.\|EXAMPLE 3\|[0070] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 litres, maintained at 35°C and agitated with a mechanical stirrer operating at 500rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its adsorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in Table 3.\|Table 3Experiment n°Total CO2 captured (mol)Slurry volume (mL)Slurry conc. (g/L)Total solids, (g)CO2 captured, as % of theoretical maximumSlurry additivesTemp. (°C)Duration (h)Solid products detected10,06412605013,0035Na2CO3: 21,15 g/L3524Hydromagnesite20,07242605013,0040Na2CO3: 53,85 g/L3524Hydromagnesite30,13632605013,0075NaHCO3: 53,85 g/L3530Hydromagnesite40,035226011,52,99843526Artinite\|[0071] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite (Mg(OH)2•4MgCO3•4H2O), and in one case artinite (Mg(OH)2•MgCO3•3H2O), which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 4\|[0072] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometre sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950°C), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio. About 5kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950°C for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by X-ray fluorescence spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3, and 33.4% sodium expressed as Na2O. An X-ray diffraction analysis showed the major phase present in the product to be Na2MgSiO4.\|EXAMPLE 5\|[0073] The reaction products of Example 2 (referred to here as "product X"), and of Example 4 (referred to here as "product XS") were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75g of the solid were added to 1.5 litres of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal litres per hour (and at close to one atmosphere absolute pressure). The reactor was maintained at 70°C by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements. The solid filter-cakes were dried at 110°C and then analysed by X-ray fluorescence spectrometry for elemental composition, by X-ray diffraction for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0074] The results for three different product samples are given in Table 4:\|Table 4Experiment N° ; anhydrous product usedDuration (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %5 Product X3.5420Hydromagnesite31.215.918.20.65961 Product X4.0600Hydromagnesite30.316.418.80.5637 Product XS4.0205Hydromagnesite27.717.219.70.471(1) In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0075] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields, of the order of 60-70% of the total magnesium in the starting material, in a time of 3.5 to 4 hours.	(EP2718230)\|[0001] This invention relates to a process for the mineralization of carbon dioxide from, for example, a gas stream such as the flue gases from an industrial combustion process. The process uses as starting material an alkali metal magnesium silicate and produces magnesium carbonate compounds and silica.\|[0002] In WO 2010/097451 magnesium-comprising silicate hydroxide particles are heated alone to activate the particles, which are then ground to a smaller size and contacted with an aqueous medium (which preferably contains a dissolved bicarbonate salt) and carbon dioxide under low temperature conditions. The solution and small activated particles are then contacted with carbon dioxide at elevated temperatures (preferably at least 140°C, and therefore under pressure to avoid the water simply boiling off).\|[0003] US2009/0202410 similarly discloses contacting an aqueous alkali metal carbonate solution with carbon dioxide to obtain a bicarbonate solution, which is then contacted with a waste material. The mineral may contain, inter alia, a magnesium-containing silicate mineral.\|[0004] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into magnesium silicate hydrate minerals such as serpentine or chlorite (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10)(OH)2).\|[0005] Magnesium silicate rocks constitute an excellent source of basic magnesium which should in theory readily be converted into stable magnesium carbonate compounds by the action of carbon dioxide gas under normal atmospheric conditions. However, in practice, the weathering and carbonation of natural magnesium silicate minerals at the Earth's surface occurs only very slowly. Thus, while the use of magnesium silicates as a source of basic magnesium for the mineralization of carbon dioxide has been proposed as a means to combat the current trend towards increasing carbon dioxide levels in the atmosphere, processes to achieve such mineralization have heretofore been excessively energy-intensive, as well as excessively expensive to set up and operate, and, and thus have not been commercialized. One of the major technical difficulties which renders such processes so expensive to set up and operate is the need to use elevated pressures and temperatures in order to achieve a sufficiently high rate (for industrial purposes) of carbonation of magnesium silicate minerals. Typically, the carbon dioxide gas must first be purified and then compressed to pressures in excess of 70 atmospheres, and then contacted with finely-ground magnesium silicates in a pressure reactor at temperatures of 120-200°C. This requires specialized equipment which is expensive to build and maintain, as well as large amounts of electric power to operate the gas purification and pressurization process as well as to finely grind the magnesium silicate rocks.\|[0006] Although the common magnesium silicate minerals listed above tend to be very "unreactive," (e.g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a "carbonate fusion", is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analysed by standard chemical techniques, thus allowing for total elemental analysis of the rock. The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0007] US 5,085,838A describes a process for reacting an asbestiform material, which may be a magnesium-containing mineral, with an alkaline flux, which may be an alkali metal carbonate, into an environmentally safe glassy material by heating to about 750°C to 1000°C. An X-ray diffraction spectrum attributes one peak to an alkali metal magnesium silicate. The glassy material produced is described as a safe, non-toxic waste, which can be disposed of, or used as a process feed-stock for producing various glassy products.\|[0008] JP2007/146094 describes the use of a water-swelling clay, named as sodium-magnesium silicate, in a detergent composition suitable for cleaning skin. The clay, which is a known material, is not a true alkali metal magnesium silicate, contains lithium as part of its structure and is known by a number of synonyms including lithium magnesium sodium salt, synthetic magnesium lithium silicate and lithium magnesium sodium silicate.\|[0009] The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step.\|[0010] The present invention accordingly provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|[0011] The alkali metal is preferably potassium or, more preferably, sodium.\|[0012] The process is preferably effected at a temperature of 25 to 100°C, more preferably 35 to 80°C. The carbon dioxide may be in the free form in a gas comprising carbon dioxide.\|[0013] The process of the invention can be used to remove carbon dioxide from a gas at a reduced or elevated pressure or, for example, at about atmospheric pressure. The process of the invention may be carried out on a carbon dioxide-containing gas at an absolute pressure generally from 0.5 to 100 bar, preferably from 1 to 20 bar, most preferably at about 1 bar.\|[0014] The gas to be treated may contain from 0.01% to 100% carbon dioxide by volume, preferably from 0.1% to 50%, more preferably from 1% to 40%, and most preferably from 4% to 30%. The gas stream may be a flue gas from an industrial combustion process.\|[0015] The carbon dioxide may also be in the form of an alkali metal carbonate or bicarbonate formed by contacting a gas comprising carbon dioxide with an alkali metal hydroxide or an alkali metal carbonate. The alkali metal carbonate or bicarbonate is preferably produced in the form of an aqueous solution, prepared by reaction between an aqueous solution of an alkali metal hydroxide or carbonate and gaseous carbon dioxide.\|[0016] The alkali metal magnesium silicate is preferably in particulate form, for example a powder, preferably having a Blaine specific surface area of 100 to 800m2/kg, more preferably 200 to 650m2/kg.\|[0017] The process according to the invention is preferably effected with a product comprising alkali metal magnesium silicate. The alkali metal magnesium silicate is preferably prepared by the reaction of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate, or a mixture thereof, with a magnesium silicate. The alkali metal carbonate compound used preferably comprises alkali metal carbonate produced by contacting a gas comprising carbon dioxide with an alkali metal magnesium silicate generally in the presence of water, the alkali metal magnesium silicate being converted into a solution of an alkali metal carbonate plus solid residues comprising magnesium carbonates and a largely amorphous product rich in silica and containing some magnesium by reaction with the carbon dioxide, and the alkali metal carbonate solution being separated and concentrated prior to reaction with the magnesium silicate.\|[0018] The invention also provides a process for the preparation of a product comprising an alkali metal magnesium silicate compound (which compound is preferably of composition R2O•MgO•SiO2, (in which R represents an alkali metal),which process comprises the reaction, at a temperature from 500 to 1100°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 2:1 to 1:2, which reaction produces the product comprising an alkali metal magnesium silicate.\|[0019] The product produced by this process may be in shaped or particulate form.\|[0020] The product may be used to provide a slurry, generally aqueous, comprising an alkali metal magnesium silicate produced by this process.\|[0021] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate expressed as silicon dioxide is preferably from 2:1 to 1:2, more preferably from 3:2 to 2:3, for example 4:3 to 3:4. The ratio is most preferably about 1.\|[0022] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used to prepare the alkali metal magnesium silicate.\|[0023] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0024] The magnesium silicate used in the preparation of the alkali metal magnesium silicate is generally a mineral silicate, for example a rock comprising a high concentration, preferably 20% or more, more preferably 50% or more, of a magnesium silicate of the general formula:\| m(MgO)•t(MeO)•SiO2•xH2O\|wherein Me represents a metal or metals other than magnesium, (such as, for example, calcium and/or iron); m is from 0.5 to 3, preferably from1 to 3, t is less than or equal to 1, and x is from zero to 2.\|[0025] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc iddingsite and hectorite. These minerals may contain substantial quantities of calcium, iron and alkali metals in addition to magnesium and silicon. Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, anthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens. The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0026] The mineral silicate used to prepare the alkali metal magnesium silicate is preferably a basic magnesium silicate. The MgO/SiO2 molar ratio is preferably from 1 to 3. The CaO/SiO2 molar ratio is preferably ≤0.5. The FeO/SiO2 molar ratio is preferably ≤0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≤0.2.\|[0027] The alkali metal carbonate compound used in the preparation of the alkali metal magnesium silicate may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2•2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g. chlorides, sulfates, sulfites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates, nitrites or hydroxides) are present which, at the temperature used to prepare the alkali metal magnesium silicate, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0028] The process used to prepare the alkali metal magnesium silicate is preferably effected at a temperature from 600 to 1000°C, for example 700 to 950°C, more preferably from 800 to 950°C. Heating is generally effected for a few minutes to a few hours, for example from 5 minutes to 24 hours, preferably from 10 minutes to 4 hours.\|[0029] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is slightly below its melting point.\|[0030] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as "R2O" in which R represents an alkali metal) present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt. = 140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt. = 106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0031] The magnesium silicate and alkali metal carbonate compound used to prepare the alkali metal magnesium silicate are preferably in particulate form or in shaped form, e.g. as pellets. Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the preparation of the alkali metal magnesium silicate will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of fine sand (grain size 0.06 to 0.2mm) or, if necessary, ground to a fine powder (grain sizes below 0.06mm). Grain sizes greater than 0.06mm are generally determined by sieving. Grain sizes lower than 0.06mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0032] In one embodiment the process to prepare the alkali metal magnesium silicate is conducted in a moving grate furnace.\|[0033] For example a mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in Figure 1 of the accompanying drawings.\|[0034] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0035] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone ("burning zone") just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate:\| (1) Mg2SiO4 + R2CO3 ⇒ product comprising R2MgSiO4 + CO2↑\|in which R is as hereinbefore defined: R preferably represents sodium.\|[0036] The vertical arrow ↑ after CO2 indicates that the carbon dioxide gas produced by this reaction escapes from the bed and exits with the rest of the exhaust gases. The idealized reaction depicted in equation (1) illustrates the production of a product comprising an alkali metal magnesium silicate by direct reaction of a stoichiometric mixture of forsterite and an alkali metal carbonate. This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 2.6 kJ (i.e. about 0.6 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, the net energy consumption for the overall process will be significant. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0037] In a further embodiment, the preparation of the alkali metal magnesium silicate is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln in a decarbonation step which produces carbon dioxide.\|[0038] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0039] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 40% of the total solids volume. In order to achieve this, it may sometimes be necessary to reduce the R2O/SiO2 ratio of the initial pellet composition to a value substantially below the preferred stoichiometric ratio of 1. The degree of reaction of the magnesium silicate during the process will then also be less than 100% but the effect of this can potentially be mitigated by separating the unreacted magnesium silicate from the reaction products and recycling it together with additional magnesium silicate starting material in the production of a fresh batch of pellets.\|[0040] According to a further feature of the invention the preparation of the alkali metal magnesium silicate is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The R2O/SiO2 ratio may be less than 1 if necessary in order to form substantially stable nodules. The nodules are decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0041] The cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate are then used in a gas scrubbing system designed to remove carbon dioxide from a gas at a reduced or elevated pressure or, for example, at about atmospheric pressure.\|[0042] In one embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are ground in water to make an aqueous suspension or slurry which can be directly injected into a conventional gas scrubbing system, such as a spray tower.\|[0043] In another embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are packed into a vertical column to form a packed bed of pellets through which a gas can be passed from bottom to top, while at the same time a suitably-controlled spray of water is added at the top of the column to ensure that the pellets remain wet. This constitutes a counter-current packed-bed gas absorber column. The flow of water leaving the bottom of this column is collected and treated as described later in more detail. The pellets or nodules used to form this type of packed bed column may be pre-selected for their dimensions and mechanical strength.\|[0044] In both of the above embodiments, the reactions occurring in the gas scrubbing system or gas absorber column are as follows:\| (2) R2MgSiO4(S) + (1+p)CO2(g) + water ⇒ (MgO)•p(CO2)•q(H2O)(s) + solid1 + R2CO3 (aq.)\|Where:\| The terms (s), (g) and (aq.) indicate solid, gas, and aqueous solution, respectively,\| p is > 0 and less than or equal to 1. Preferably, p is greater than or equal to 0.5\| q may be zero but can also take values as high as 3 in some cases.\|[0045] The principal solid products are:\| a magnesium carbonate compound, (MgO)•p(CO2)•q(H2O), which may contain more than one chemical compound, and in which a significant fraction of the carbon dioxide captured from the gas stream is contained in a stable solid form; and\| solid1 which is a largely amorphous solid rich in silica and containing some magnesium.\|[0046] These two principal solid products will generally be intimately mixed.\|[0047] Other minor solid products that may also be present include iron oxides, hydroxides or carbonates, as well as calcium carbonates.\|[0048] The alkali metal carbonate solution resulting from the gas scrubbing process will, if reaction (2) goes to completion, contain all of the alkali metal ions present in the original solid product. It is therefore desirable to separate this alkali metal carbonate solution and extract the alkali metal carbonates in solid form for re-use in the high temperature process according to reaction (1). In principle, this can be done most effectively by a combination of evaporation and crystallization processes, making use of the waste heat available both from the decarbonation reaction (1) and also from the flue gas scrubbing system, (noting that reactions (2) and (3) are both highly exothermic and thus that the gas scrubbing system itself is likely to operate at a higher temperature than the temperature of the flue gases being treated by it, thus producing a hot solution of alkali metal carbonate).\|[0049] Some other salts may be present in the alkali metal carbonate solution due to impurities in the magnesium silicate rocks or the flue gases. The most common impurities are likely to be alkali metal sulfates, sulfites, nitrates and nitrites. Under certain circumstances it may be necessary to separate these salts from the recycled alkali metal carbonate by specialized crystallization and washing procedures.\|[0050] In yet another embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are crushed, and if necessary ground, to a suitable median particle size. They are then contacted with a solution comprising an alkali metal bicarbonate in, for example, a tank, preferably with some mechanical stirring. The alkali metal bicarbonate solution may originate from a gas scrubbing system designed to capture carbon dioxide from a gas at, for example, atmospheric pressure. Typical reactions between the alkali-metal bicarbonate solution and the solids in this case is shown by the following equations:\| (3) R2MgSiO4(s) + 2(1+p)RHCO3(aq.) + water ⇒ (MgO)•p(CO2)•q(H2O)(s) + solid1 + (2+p)R2CO3 (aq.)\|[0051] The solid1 is as described above.\|[0052] The alkali metal bicarbonate solution (RHCO3(aq.)) used in reaction (3) may be formed by the reaction of the alkali metal carbonate solution (R2CO3(aq.)) produced in reaction (3) with carbon dioxide and water as shown in reaction (4):\| (4) R2CO3 (aq.) + CO2(g) + water ⇒ 2RHCO3(aq.)\|[0053] This reaction can be conducted in a separate gas scrubbing system, thus participating in a closed-loop alkali-carbonate/bicarbonate gas scrubbing system.\|[0054] The reactions described above are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid magnesium carbonate compounds. The magnesium carbonate solid produced may comprise either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or complex magnesium hydroxy-carbonate hydrates, such as artinite (Mg(OH)2•MgCO3•3H2O), or hydromagnesite, (Mg(OH)2•4MgCO3•4H2O), depending on the conditions. All of these precipitated solids, plus the solid1, will in many cases be finer than the unreacted starting material (Mg2SiO4 in this example), and so could be separated from it by sedimentation and then separated from the alkali metal carbonate which remains in solution by filtration. The unreacted starting material (Mg2SiO4 in this case) thus separated can be recycled to the beginning of the process. The alkali metal carbonate solution can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and also recycled to the start of the process. The mixture of magnesium carbonates and largely amorphous product rich in silica and containing some magnesium produced by these reactions is one of the final products of the overall process (and constitutes a feature of the invention) and can be separated for disposal or for use in other processes.\|[0055] One overall object of the process of the invention is to use common magnesium silicate rocks to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable magnesium carbonate compound.\|[0056] An example of a process of the invention which seeks to maximise capture of CO2 from exhaust gases from other industrial processes and to convert it substantially completely into solid magnesium carbonates in an energy-efficient way, not requiring any high-pressure reactors or autoclaves of the type usually required for direct carbonation of magnesium silicates, is shown in Figure 2 (in which solid1 is a largely amorphous product rich in silica and containing some magnesium).\|[0057] Raw materials are prepared to form a mixture of one part of a magnesium silicate (mMgO.SiO2.xH2O) plus another part being a combination of one or more alkali metal carbonate compounds for which the combined composition is represented by the formula (R2O.nCO2.yH2O); the mixture is heated by fuel combustion gases from a burner supplied with fuel and air; the heated mixture reacts to form a product comprising an alkali metal magnesium silicate (R2O.MgO.SiO2) and to release carbon dioxide which mixes with the fuel combustion gases to form exhaust gases with excess carbon dioxide; liquid water is added to the reaction product and the product is wet ground to form a slurry; the slurry is contacted in a gas scrubber with the exhaust gases with excess carbon dioxide produced earlier and with CO2-containing exhaust gases from other processes to absorb carbon dioxide and to produce a slurry comprising magnesium carbonate and silicon dioxide; the slurry is filtered to produce a filtercake comprising magnesium carbonate and a largely amorphous product rich in silica and containing some magnesium; the filter-cake is dried to produce a mixed solid product which is dried; the filtrate comprising alkali metal carbonate compound in solution is dried or crystallized to produce solid alkali metal carbonate compound which is recycled for use as starting material.\|[0058] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0059] The term "pellets" as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0060] Particle size and size distribution when measured by laser granulometry for particle sizes less than about 100µm are measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He-Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.The apparatus is checked before each working session by means of a standard sample (Sifraco C10 silica) for which the particle size distribution is known.\|[0061] Measurements are performed with the following parameters: pump speed 2300rpm and stirrer speed 800rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30s (for possible air bubbles to clear), a measurement is carried out for 15s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0062] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0063] Particle sizes and particle size distributions for particle sizes greater than about 100µm are measured by sieving.\|[0064] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R, m, t, x, p, n, z and y are as initially defined.\|[0065] The following non-limiting Examples illustrate embodiments of the invention.\|EXAMPLE 1\|[0066] Ground olivine sand of composition (Mg0.94Fe0.06)2SiO4 was mixed with a sodium carbonate hydrate powder in a 14:11 mass ratio. 25g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800°C over 2 hours, maintained at 800°C for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table 1:\|Table 1SampleLoss on IgnitionSodium carbonate powder14.97 %Ground olivine sand0.22 %14:11 mix of ground olivine sand + sodium carbonate powder16.69 %\|[0067] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by X-ray diffraction. The reaction products observed by this technique included Na2MgSiO4 and Fe2O3 together with some unreacted olivine and sodium carbonate.\|EXAMPLE 2\|[0068] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. (The molar ratio of this mixture is close to 1). The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900°C. The sample was air-quenched after 1h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851 °C). The measured loss on ignition of all of the samples is presented in the following Table 2 :\|Table 2SampleLoss on IgnitionSodium carbonate14.96 %Olivine0.04 %Olivine + Sodium carbonate23.02 %\|[0069] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by X-ray diffraction and the main phases detected included Na2MgSiO4, together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data.\|EXAMPLE 3\|[0070] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 litres, maintained at 35°C and agitated with a mechanical stirrer operating at 500rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its adsorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in Table 3.\|Table 3Experiment n°Total CO2 captured (mol)Slurry volume (mL)Slurry conc. (g/L)Total solids, (g)CO2 captured, as % of theoretical maximumSlurry additivesTemp. (°C)Duration (h)Solid products detected10,06412605013,0035Na2CO3: 21,15 g/L3524Hydromagnesite20,07242605013,0040Na2CO3: 53,85 g/L3524Hydromagnesite30,13632605013,0075NaHCO3: 53,85 g/L3530Hydromagnesite40,035226011,52,99843526Artinite\|[0071] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite (Mg(OH)2•4MgCO3•4H2O), and in one case artinite (Mg(OH)2•MgCO3•3H2O), which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 4\|[0072] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometre sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950°C), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio. About 5kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950°C for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by X-ray fluorescence spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3, and 33.4% sodium expressed as Na2O. An X-ray diffraction analysis showed the major phase present in the product to be Na2MgSiO4.\|EXAMPLE 5\|[0073] The reaction products of Example 2 (referred to here as "product X"), and of Example 4 (referred to here as "product XS") were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75g of the solid were added to 1.5 litres of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal litres per hour (and at close to one atmosphere absolute pressure). The reactor was maintained at 70°C by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements. The solid filter-cakes were dried at 110°C and then analysed by X-ray fluorescence spectrometry for elemental composition, by X-ray diffraction for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0074] The results for three different product samples are given in Table 4:\|Table 4Experiment N° ; anhydrous product usedDuration (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %5 Product X3.5420Hydromagnesite31.215.918.20.65961 Product X4.0600Hydromagnesite30.316.418.80.5637 Product XS4.0205Hydromagnesite27.717.219.70.471(1) In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0075] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields, of the order of 60-70% of the total magnesium in the starting material, in a time of 3.5 to 4 hours.	Family Number\|(15065813)\|15065813\|Object of Invention\|(EP2532624 A1)\|The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(WO2012168176 A1)\|The present invention seeks to provide a process for the capture of carbon dioxide (C02) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(EP2718230 B1)\|The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(CA2838035 A1)\|The present invention seeks to provide a process for the capture of carbon dioxide (00 2 ) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(CN103582611B B)\|The present invention seeks to provide a method for capturing carbon dioxide ( CO ) by using alkali magnesium silicate which can be made from magnesium silicate rock and which can be carried out , for example , at atmospheric pressure2 ) And / or is capable of removing di directly from a typical industrial flue gas stream without any pre - concentration stepA method for oxidizing carbon . \|(CN103582611 A)\|The present invention seeks to provide a method for capturing carbon dioxide ( CO ) by using alkali magnesium silicate which can be made from magnesium silicate rock and which can be carried out , for example , at atmospheric pressure2 ) And / or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre - concentration step . \|(US20140120022 A1)\|The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(KR20140045459 A)\| (...) dioxide directly from typical industrial flue gas streams without any preconcentration steps and/or by a process which can be carried out, for example, at atmospheric pressure, using alkali metal magnesium silicate which can be produced from rock magnesium silicate,2) of the present invention.\|Advantages / Prev. Drawbacks\|(CN103582611B B)\|This requires specialized equipment that is expensive to build and maintain , and also requires a large amount of electricity to operate the gas purification and pressurization process and to finely grind the magnesium silicate rock .\|(CN103582611 A)\|This requires specialized equipment that is expensive to build and maintain , and also requires a large amount of electricity to operate the gas purification and pressurization process and to finely grind the magnesium silicate rock .\|	Environmental technology\|Materials, metallurgy	B01D-053/14\|B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-2251/304\|B01D-2251/306\|B01D-2251/402\|B01D-2251/60\|B01D-2251/604\|B01D-2251/606\|B01D-2257/504\|B01D-2258/0283\|C01B-033/22\|C01B-033/32\|C01F-005/24\|Y02C-010/04\|Y02C-010/06\|Y02C-020/40\|Y02P-020/151\|Y02P-020/152		B01D-053/14\|B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-2251/304\|B01D-2251/306\|B01D-2251/402\|B01D-2251/60\|B01D-2251/604\|B01D-2251/606\|B01D-2257/504\|B01D-2258/0283\|C01B-033/22\|C01B-033/32\|C01F-005/24\|Y02C-010/04\|Y02C-010/06\|Y02C-020/40\|Y02P-020/151\|Y02P-020/152	B01D-053/14\|B01D-053/62\|B01D-053/78\|B01D-053/80\|C01B-033/22\|C01B-033/32\|C01F-005/24	B01D-053/14\|B01D-053/62\|B01D-053/78\|B01D-053/80\|C01B-033/22\|C01B-033/32\|C01F-005/24	PCLO=423331000\|PCLX=423430000	PCLO=423331000 PCLX=423430000	EP2925426\|WO201482996\|WO202662133\|EP2735553;EP2735553\|EP2735555\|WO2024156118\|CN114334032\|CN114390943\|WO2024200557\|DE102023108019\|DE102023108019\|US12258296\|US11718558\|US12110601\|US11839849\|EP4178927\|WO202212795\|CN114728848B\|EP3939945\|AU2013351282;AU2013351282\|US9631257	EP2925426 66131709 WHO=Examiner SELF=Y CAT=X CAT=P CAT=I\|WO201482996 66131709 WHO=Examiner SELF=Y CAT=X CAT=P CAT=I\|WO202662133 118233234 WHO=Examiner SELF=N CAT=X CAT=I\|EP2735553 66070146 WHO=Examiner SELF=N CAT=E\|EP2735555 66070145 WHO=Examiner SELF=N CAT=E\|WO2024156118 104821837 WHO=Examiner SELF=N CAT=A\|CN114334032 99582529 WHO=Examiner SELF=N CAT=A\|CN114390943 92128920 WHO=Examiner SELF=N CAT=A\|WO2024200557 111675593 WHO=Applicant SELF=N\|DE102023108019 111675593 WHO=Examiner SELF=N\|DE102023108019 111675593 WHO=Applicant SELF=N\|US12258296 104821837 WHO=Applicant SELF=N\|US11718558 92777983 WHO=Applicant SELF=N\|US12110601 86698390 WHO=Applicant SELF=N\|US11839849 100984116 WHO=Examiner SELF=N\|EP4178927 98313250 WHO=Applicant SELF=N\|WO202212795 98313250 WHO=Applicant SELF=N\|CN114728848B 93726190 WHO=Examiner SELF=N\|EP3939945 98313250 WHO=Applicant SELF=N\|AU2013351282 66131709 WHO=Examiner SELF=Y\|US9631257 66131709 WHO=Applicant SELF=Y	WO201097451\|WO201097451\|US20090202410\|US20090202410\|US5085838\|US5085838\|WO201097451\|US20090202410\|US5085838\|JP2007146094\|JP2007146094\|JP2007146094\|US20100196235\|US20100196235\|US20100196235\|WO201097451\|WO201097451\|CN101596397\|US20090202410\|US20090202410\|US20090202410\|US20100196235\|CN101356118\|JP2007146094\|JP2007146094\|US5085838\|US5085838\|US5085838	WO201097451 44611783 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|WO201097451 44611783 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|US20090202410 4163858 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|US20090202410 4163858 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|US5085838 42717873 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|US5085838 42717873 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|WO201097451 44611783 WHO=Examiner SELF=N CAT=X CAT=A CAT=I\|US20090202410 4163858 WHO=Examiner SELF=N CAT=X CAT=A CAT=I\|US5085838 42717873 WHO=Examiner SELF=N CAT=X CAT=A CAT=I\|JP2007146094 32582907 WHO=Examiner SELF=N CAT=X\|JP2007146094 32582907 WHO=Examiner SELF=N CAT=X\|JP2007146094 32582907 WHO=Examiner SELF=N CAT=X\|US20100196235 1841774 WHO=Examiner SELF=N CAT=A\|US20100196235 1841774 WHO=Examiner SELF=N CAT=A\|US20100196235 1841774 WHO=Examiner SELF=N CAT=A\|WO201097451 44611783 WHO=Applicant SELF=N\|WO201097451 44611783 WHO=Applicant SELF=N\|CN101596397 6876258 WHO=Examiner SELF=N\|US20090202410 4163858 WHO=Applicant SELF=N\|US20090202410 4163858 WHO=Applicant SELF=N\|US20090202410 4163858 WHO=Examiner SELF=N\|US20100196235 1841774 WHO=Applicant SELF=N\|CN101356118 6679764 WHO=Examiner SELF=N\|JP2007146094 32582907 WHO=Applicant SELF=N\|JP2007146094 32582907 WHO=Applicant SELF=N\|US5085838 42717873 WHO=Applicant SELF=N\|US5085838 42717873 WHO=Applicant SELF=N\|US5085838 42717873 WHO=Examiner SELF=N		JP2007146094; US20100196235; WO201097451; US20090202410; US5085838\|JP2007146094; US20100196235; WO201097451; US20090202410; US5085838; WO201097451; US20090202410; US5085838; JP2007146094\|\|US5085838; US20090202410; CN101596397; CN101356118\|US5085838; US20090202410; US20100196235; JP2007146094; WO201097451\|\|\|JP2007146094; US20100196235; WO201097451; US20090202410; US5085838	(EP2718230)\|Examiner references\|-See also references of WO 2012168176A1\|\|\|(US9469546)\|Applicant references\|-International Search Report as issued for International Application No. PCT/EP2012/060480, dated Jul. 31, 2012.\|-International Preliminary Report on Patentability as issued for International Application No. PCT/EP2012/060480, dated Dec. 27, 2013.\|\|\|\|\|\|	GRANTED	(EP2718230)\|GRANTED\|(EP2532624)\|LAPSED\|(US9469546)\|LAPSED\|(WO2012/168176)\|LAPSED\|(CN103582611)\|LAPSED\|(HRP20180851)\|LAPSED\|(KR10-2014-0045459)\|LAPSED\|(CA2838035)\|LAPSED	ALIVE	(EP2718230)\|ALIVE\|(EP2532624)\|DEAD\|(US9469546)\|DEAD\|(WO2012/168176)\|DEAD\|(CN103582611)\|DEAD\|(HRP20180851)\|DEAD\|(KR10-2014-0045459)\|DEAD\|(CA2838035)\|DEAD	(EP2718230)\|LEGAL DETAILS FOR EP2718230\|Actual or expected expiration date=2032-06-04\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2012-06-04\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP12727348\|Application date=2012-06-04\|Standardized application number=2012EP-0727348\|Event publication date=2014-03-14\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2014-04-16\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2718230\|Publication stage code=A1\|Publication date=2014-04-16\|Standardized publication number=EP2718230\|Event publication date=2014-04-16\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2014-01-07\|Event publication date=2014-04-16\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2014-09-10\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2017-05-03\|Event code=EP/17Q\|Event indicator=Pos\|Event group=Examination events\|First examination report\|Erster pruefungsbescheid\|Effective date of the event=2017-03-31\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-18\|Event code=EP/GRAP\|Event indicator=Pos\|Event group=Examination events\|DESPATCH OF COMMUNICATION OF INTENTION TO GRANT A PATENT\|New entry: communication of intention to grant a patent\|Original code: EPIDOSNIGR1\|Event publication date=2017-11-15\|Event code=EP/INTG\|Event indicator=Pos\|Event group=Examination events\|Announcement of intention to grant\|Effective date of the event=2017-10-19\|Event publication date=2018-02-22\|Event code=EP/GRAS\|Event indicator=Pos\|Event group=Examination events Payment or non-payment notifications\|GRANT FEE PAID\|New entry: payment of fee for grant\|Original code: EPIDOSNIGR3\|Event publication date=2018-03-02\|Event code=EP/GRAJ\|Event group=Examination events\|INFORMATION RELATED TO DISAPPROVAL OF COMMUNICATION OF INTENTION TO GRANT BY THE APPLICANT OR RESUMPTION OF EXAMINATION PROCEEDINGS BY THE EPO DELETED\|Deletion - disapproval of the communication of intention to grant the patent by the applicant or resumption of examination proceedings by the EPO\|Original code: EPIDOSDIGR1\|Event publication date=2018-03-02\|Event code=EP/GRAL\|Event group=Examination events\|INFORMATION RELATED TO PAYMENT OF FEE FOR PUBLISHING/PRINTING DELETED\|Deletion: payment of fee for publishing/printing\|Original code: EPIDOSDIGR3\|Event publication date=2018-04-04\|Event code=EP/INTC\|Event group=Examination events\|Former communication of intention to grant cancelled\|Event publication date=2018-04-11\|Event code=EP/GRAR\|Event indicator=Pos\|Event group=Examination events\|INFORMATION RELATED TO INTENTION TO GRANT A PATENT RECORDED\|New entry: information about intention to grant a patent\|Original code: EPIDOSNIGR71\|Event publication date=2018-04-20\|Event code=EP/GRAA\|Event indicator=Pos\|Event group=Examination events\|(EXPECTED) GRANT\|Original code: 0009210\|Event publication date=2018-05-16\|Event code=EP/INTG\|Event indicator=Pos\|Event group=Examination events\|Announcement of intention to grant\|Effective date of the event=2018-04-11\|Event publication date=2018-05-23\|Event code=EP/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent specification\|Publication country=EP\|Publication number=EP2718230\|Publication stage code=B1\|Publication date=2018-05-23\|Standardized publication number=EP2718230\|Event publication date=2018-05-23\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2018-10-31\|Event code=EP/RAP2\|Event group=Change of name or address Reassignment\|Rights of a patent transferred\|Patentinhaber uebertragung (korr.)\|OWNER:HOLCIM TECHNOLOGY LTD.\|Event publication date=2019-03-29\|Event code=EP/PLBE\|Event indicator=Pos\|Event group=No opposition filed\|NO OPPOSITION FILED WITHIN TIME LIMIT\|Original code: 0009261\|Event publication date=2019-03-29\|Event code=EP/STAANOPP\|Event indicator=Pos\|Event group=No opposition filed Event indicating In Force\|No opposition filed within time limit\|Original code: STAA\|Event publication date=2019-05-01\|Event code=EP/26N\|Event indicator=Pos\|Event group=No opposition filed Event indicating In Force\|No opposition filed\|Kein einspruch eingelegt\|Effective date of the event=2019-02-26\|MEMBER STATE LEGAL DETAILS FOR AL\|Actual or expected expiration date=2019-11-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=AL\|Event publication date=2019-11-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=AL\|MEMBER STATE LEGAL DETAILS FOR AT\|Actual or expected expiration date=2032-06-04\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=AT Corresponding appl: AT1001087\|Event publication date=2018-06-15\|Event code=EP/REG\|Event code=AT/REF\|Event indicator=Pos\|Event group=Entry into national phase\|Reference to a national code\|Reference to at number (ep patent enters austrian national phase)\|Nennung der e-nummer (EP patent tritt in at nationale phase ein)\|Effective date of the event=2018-06-15\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2018-08-30\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-08-30\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2019-09-15\|Event code=EP/REG\|Event code=AT/PC\|Event group=Change of name or address Reassignment\|Reference to a national code\|Change of the owner\|Aenderung an der person des patentinhabers\|OWNER:HOLCIM TECHNOLOGY LTD, CH\|Effective date of the event=2019-08-02\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2020-02-15\|Event code=EP/REG\|Event code=AT/MM01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Lapse because of not paying annual fees\|Loeschung wegen nichtzahlung der jaehrlichen gebuehr\|Effective date of the event=2019-06-04\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2020-05-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2021-07-15\|Event code=EP/REG\|Event code=AT/UEP\|Event indicator=Pos\|Event group=Examination events Entry into national phase\|Reference to a national code\|Publication of translation of european patent specification\|Uebersetzung der europaeischen patentschrift ausgegeben\|Effective date of the event=2018-05-23\|Corresponding cc:\|Designated or member state=AT\|MEMBER STATE LEGAL DETAILS FOR BE\|Actual or expected expiration date=2018-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BE\|Event publication date=2019-03-06\|Event code=EP/REG\|Event code=BE/MM\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|LAPSED BECAUSE OF NON-PAYMENT OF THE ANNUAL FEE\|Effective date of the event=2018-06-30\|Corresponding cc:\|Designated or member state=BE\|Event publication date=2019-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=BE\|MEMBER STATE LEGAL DETAILS FOR BG\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BG\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=BG\|MEMBER STATE LEGAL DETAILS FOR CH\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2018-05-31\|Event code=EP/REG\|Event code=CH/EP\|Event indicator=Pos\|Event group=Entry into national phase\|Reference to a national code\|EUROPEAN PATENT TAKES EFFECT AS A NATIONAL PATENT IN CH/LI\|Wirkung des europäischen patents als nationales patent in ch/li tritt ein\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2019-01-31\|Event code=EP/REG\|Event code=CH/PL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent ceased\|Loeschung/radiation/radiazion\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2019-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=CH\|MEMBER STATE LEGAL DETAILS FOR CY\|Actual or expected expiration date=2020-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CY\|Event publication date=2020-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=CY\|MEMBER STATE LEGAL DETAILS FOR CZ\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CZ\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=CZ\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2020-01-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE Corresponding appl: DE602012046594\|Event publication date=2017-09-06\|Event code=EP/REG\|Event code=DE/R079\|Event group=Corrections\|Reference to a national code\|Amendment of ipc main class\|Aenderung der IPC hauptklasse\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2017-09-06\|Event code=EP/REG\|Event code=DE/R079\|Event group=Corrections\|Reference to a national code\|Amendment of ipc main class\|Aenderung der IPC hauptklasse\|Previous main class: C01B0033220000\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-06-21\|Event code=EP/REG\|Event code=DE/R096\|Event indicator=Pos\|Event group=Examination events\|Reference to a national code\|DPMA publication of mentioned EP patent grant\|Veroeffentlichung eines hinweises auf die ep-patenterteilung durch das dpma\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-06-27\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-06-27\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-09-20\|Event code=EP/REG\|Event code=DE/R082\|Event group=Examination events\|Reference to a national code\|Change of representative\|Aenderung des vertreters\|REPRESENTATIVE:BEETZ & PARTNER MBB PATENT- UND RECHTSANWAELTE, DE\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-09-20\|Event code=EP/REG\|Event code=DE/R081\|Event group=Examination events Reassignment\|Reference to a national code\|Change of applicant/patentee\|Aenderung des anmelders/inhabers\|Former owner: LAFARGE, PARIS, FR\|OWNER:HOLCIM TECHNOLOGY LTD., CH\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-09-20\|Event code=EP/REG\|Event code=DE/R082\|Event group=Examination events\|Reference to a national code\|Change of representative\|Aenderung des vertreters\|REPRESENTATIVE:BEETZ & PARTNER MBB PATENTANWAELTE, DE\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2019-02-26\|Event code=EP/REG\|Event code=DE/R097\|Event indicator=Pos\|Event group=No opposition filed\|Reference to a national code\|No opposition filed against granted patent, or EPO opposition proceedings concluded without decision\|Gegen die patenterteilung wurde kein einspruch erhoben, bzw. einspruchsverfahren ist beim epa ohne entscheidung abgeschlossen\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2020-01-01\|Event code=EP/REG\|Event code=DE/R119\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Application deemed withdrawn, or ip right lapsed, due to non-payment of renewal fee\|Die anmeldung gilt als zurueckgenommen wegen nichtzahlung der jahresgebuehr / schutzrecht ist wegen nichtzahlung der jahresgebuehr verfallen\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2020-05-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR DK\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DK\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=DK\|MEMBER STATE LEGAL DETAILS FOR EE\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EE\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=EE\|MEMBER STATE LEGAL DETAILS FOR ES\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=ES\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=ES\|MEMBER STATE LEGAL DETAILS FOR FI\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=FI\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=FI\|MEMBER STATE LEGAL DETAILS FOR FR\|Actual or expected expiration date=2020-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2018-06-26\|Event code=EP/REG\|Event code=FR/PLFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications Restitution or restoration\|Reference to a national code\|Fee payment\|Derniere annuite payee\|Annual fees payment date=2018-06-26\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2018-06-26\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-06-26\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2020-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=FR\|MEMBER STATE LEGAL DETAILS FOR GB\|Actual or expected expiration date=2018-08-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2018-05-23\|Event code=EP/REG\|Event code=GB/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patent granted\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2018-08-23\|Event code=EP/GBPC\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|GB: European patent ceased through non-payment of renewal fee\|Effective date of the event=2018-08-23\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2019-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=GB\|MEMBER STATE LEGAL DETAILS FOR GR\|Actual or expected expiration date=2020-05-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GR Corresponding appl: GR20180401871\|Event publication date=2018-07-19\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-07-19\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=GR\|Event publication date=2019-01-25\|Event code=EP/REG\|Event code=GR/EP\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|Ep patent validated in greece\|Effective date of the event=2019-01-09\|Corresponding cc:\|Designated or member state=GR\|Event publication date=2020-05-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=GR\|MEMBER STATE LEGAL DETAILS FOR HRP20180851\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HR Corresponding appl: HRP20180851\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2018HR-0000851\|Corresponding cc:\|Designated or member state=HR Corresponding pat: HRP20180851\|Publication stage code in the designated or member state=T1\|Publication date in the designated or member state=2018-06-29\|Publication number in the designated or member state=HRP20180851\|Event publication date=2018-05-29\|Event code=EP/REG\|Event code=HR/TUEP\|Event group=Administrative notifications\|Reference to a national code\|REQUEST FOR EP VALIDATION RECEIVED\|Uredan zahtjev za upis (prosirenog) europskog patenta\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2018-06-11\|Event code=EP/REG\|Event code=HR/ODRP\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|Reference to a national code\|RENEWAL FEE FOR THE MAINTENANCE OF A PATENT\|Odrzavanje patenta u vrijednosti\|Annual fees payment date=2018-06-11\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2018-06-11\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-06-11\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2018-06-29\|Event code=EP/REG\|Event code=HR/T1PR\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|EP PATENT VALIDATED IN CROATIA\|Ep patent validiran u hrvatskoj\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2019-02-05\|Event code=EP/REG\|Event code=HR/PPPP\|Event group=Reassignment\|Reference to a national code\|TRANSFER OF RIGHTS\|Prijenos prava\|OWNER:HOLCIM TECHNOLOGY LTD, CH\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2019-06-04\|Event code=EP/REG\|Event code=HR/PBON\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Reference to a national code\|LAPSE DUE TO NON-PAYMENT OF RENEWAL FEE\|Prestanak vrijednosti patenata zbog neodrzavanja\|Effective date of the event=2019-06-04\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2020-05-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=HR\|MEMBER STATE LEGAL DETAILS FOR HU\|Actual or expected expiration date=2020-05-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HU\|Event publication date=2020-05-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO\|Corresponding cc:\|Designated or member state=HU\|MEMBER STATE LEGAL DETAILS FOR IE\|Actual or expected expiration date=2019-03-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2018-06-13\|Event code=EP/REG\|Event code=IE/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patents granted designating Ireland\|European patent granted\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2019-03-20\|Event code=EP/REG\|Event code=IE/MM4A\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent lapsed\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2019-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=IE\|MEMBER STATE LEGAL DETAILS FOR IS\|Actual or expected expiration date=2020-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IS\|Event publication date=2020-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IS\|MEMBER STATE LEGAL DETAILS FOR IT\|Actual or expected expiration date=2020-05-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2018-08-22\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-08-22\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2020-05-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=IT\|MEMBER STATE LEGAL DETAILS FOR LI\|Actual or expected expiration date=2019-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LI\|Event publication date=2019-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LI\|MEMBER STATE LEGAL DETAILS FOR LT\|Actual or expected expiration date=2018-10-10\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2018-10-10\|Event code=EP/REG\|Event code=LT/MG4D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Invalidated european patent\|Europos patentai, laikomi ab initio negaliojanciais\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LT\|MEMBER STATE LEGAL DETAILS FOR LU\|Actual or expected expiration date=2019-03-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LU\|Event publication date=2019-03-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LU\|MEMBER STATE LEGAL DETAILS FOR LV\|Actual or expected expiration date=2018-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LV\|Event publication date=2018-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LV\|MEMBER STATE LEGAL DETAILS FOR MC\|Actual or expected expiration date=2019-03-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MC\|Event publication date=2019-03-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MC\|MEMBER STATE LEGAL DETAILS FOR MK\|Actual or expected expiration date=2020-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MK\|Event publication date=2020-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=MK\|MEMBER STATE LEGAL DETAILS FOR MT\|Actual or expected expiration date=2020-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MT\|Event publication date=2020-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=MT\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=2018-05-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2018-09-26\|Event code=EP/REG\|Event code=NL/MP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent voided (invalid in the netherlands as no translation has been filed)\|Effective date of the event=2018-05-23\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2018-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NL\|MEMBER STATE LEGAL DETAILS FOR NO\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NO\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NO\|MEMBER STATE LEGAL DETAILS FOR PL\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PL\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PL\|MEMBER STATE LEGAL DETAILS FOR PT\|Actual or expected expiration date=2020-05-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PT\|Event publication date=2020-05-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PT\|MEMBER STATE LEGAL DETAILS FOR RO\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RO\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RO\|MEMBER STATE LEGAL DETAILS FOR RS\|Actual or expected expiration date=2018-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RS\|Event publication date=2018-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RS\|MEMBER STATE LEGAL DETAILS FOR SE\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SE\|MEMBER STATE LEGAL DETAILS FOR SI\|Actual or expected expiration date=2019-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SI\|Event publication date=2019-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SI\|MEMBER STATE LEGAL DETAILS FOR SK\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SK\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SK\|MEMBER STATE LEGAL DETAILS FOR SM\|Actual or expected expiration date=2019-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SM\|Event publication date=2019-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SM\|MEMBER STATE LEGAL DETAILS FOR TR\|Actual or expected expiration date=2020-03-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=TR\|Event publication date=2020-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=TR\|(EP2532624)\|LEGAL DETAILS FOR EP2532624\|Actual or expected expiration date=2017-07-15\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-06-07\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP11305696\|Application date=2011-06-07\|Standardized application number=2011EP-0305696\|Event publication date=2012-12-11\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2012-12-12\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2532624\|Publication stage code=A1\|Publication date=2012-12-12\|Standardized publication number=EP2532624\|Event publication date=2012-12-12\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2012-12-12\|Event code=EP/AX\|Event indicator=Pos\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT\|Request for extension of the european patent to\|Designated contracting states=BA ME\|Event publication date=2013-07-24\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2013-06-12\|Event publication date=2013-07-24\|Event code=EP/RBV\|Event indicator=Pos\|Event group=Designated states Corrections\|Designated contracting states (correction):\|Benannte vertragsstaaten (korr.)\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2017-05-03\|Event code=EP/17Q\|Event indicator=Pos\|Event group=Examination events\|First examination report\|Erster pruefungsbescheid\|Effective date of the event=2017-04-03\|Event publication date=2017-12-22\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2018-01-24\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2017-07-15\|(US9469546)\|LEGAL DETAILS FOR US9469546\|Actual or expected expiration date=2020-11-23\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US14123987\|Application date=2012-06-04\|Standardized application number=2012US-14123987\|Event publication date=2012-06-04\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:BERNS, DANIEL J\|Event publication date=2012-06-04\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2012-06-04\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 035112-0428430\|Event publication date=2012-06-04\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 909\|Event publication date=2012-06-04\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2012-06-04\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2013-12-05\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:GARTNER, ELLIS;PISCH, ALEXANDER;SIGNING DATES FROM 20131122 TO 20131126\|Reel/frame:031720/0728\|OWNER:LAFARGE, FRANCE\|Event publication date=2013-12-05\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2013-12-05\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2013-12-05\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2014-01-10\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2014-01-24\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2014-01-24\|Event code=US/M903\|Event indicator=Pos\|Event group=Examination events OAO\|Notice of DO/EO Acceptance Mailed\|Event publication date=2014-02-26\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2014-05-01\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20140120022\|Publication stage code=A1\|Publication date=2014-05-01\|Standardized publication number=US20140120022\|Event publication date=2014-05-01\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2015-11-15\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2015-11-19\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2015-11-19\|R4R=102b\|RJST=non-final\|Rejected claims 1-12\|RJCT=WO2010097451\|Event publication date=2015-11-19\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2015-11-19\|R4R=112b\|RJST=non-final\|Rejected claims 5-8 and 10-12; 5; 10\|Event publication date=2016-02-19\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2016-06-02\|Event code=US/EXET\|Event group=Examination events OAO INT\|Interview Summary - Examiner Initiated - telephonic\|Event publication date=2016-06-13\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2016-06-17\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2016-09-13\|Event code=US/NOARR\|Event group=Examination events\|Response to Reasons for Allowance\|Event publication date=2016-09-13\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2016-09-13\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2016-09-14\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2016-09-28\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2016-10-18\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US09469546\|Publication stage code=B2\|Publication date=2016-10-18\|Standardized publication number=US9469546\|Event publication date=2016-10-18\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 283 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=283\|Event publication date=2019-01-18\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignor:LAFARGE\|Reel/frame:048061/0707\|OWNER:HOLCIM TECHNOLOGY LTD, SWITZERLAND\|Effective date of the event=2018-12-10\|Event publication date=2019-10-29\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2020-06-08\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2020-10-18\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2020-10-18\|Event publication date=2020-11-23\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2020-11-23\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|Event publication date=2023-10-31\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|(WO2012/168176)\|LEGAL DETAILS FOR WO2012/168176\|Actual or expected expiration date=2014-12-07\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOEP2012/060480\|Application date=2012-06-04\|Standardized application number=2012WO-EP60480\|Event publication date=2012-12-13\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2012/168176\|Publication stage code=A1\|Publication date=2012-12-13\|Standardized publication number=WO2012168176\|Event publication date=2014-12-07\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR CA2838035\|Actual or expected expiration date=2020-08-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA2838035\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2012CA-2838035\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA2838035\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2012-12-13\|Publication number in the designated or member state=CA2838035\|Event publication date=2013-12-03\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=CA\|Event publication date=2020-11-07\|Event code=CA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR CN103582611\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN201280027687\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2012CN-80027687\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN103582611\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2014-02-12\|Publication number in the designated or member state=CN103582611\|Event publication date=2020-05-22\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2013-12-09\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2013-12-09\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP2718230\|Actual or expected expiration date=2032-06-04\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP12727348\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2012EP-0727348\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2718230\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2014-04-16\|Publication number in the designated or member state=EP2718230\|Event publication date=2013-02-06\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2013-11-20\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2019-05-01\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR HRP20180851\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HR Corresponding appl: HRP20180851\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2018HR-0000851\|Corresponding cc:\|Designated or member state=HR Corresponding pat: HRP20180851\|Publication stage code in the designated or member state=T1\|Publication date in the designated or member state=2018-06-29\|Publication number in the designated or member state=HRP20180851\|Event publication date=2018-06-29\|Event code=HR/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=HR\|MEMBER STATE LEGAL DETAILS FOR KR10-2014-0045459\|Actual or expected expiration date=2017-07-05\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=KR Corresponding appl: KR20137035129\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2013KR-7035129\|Corresponding cc:\|Designated or member state=KR Corresponding pat: KR10-2014-0045459\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2014-04-16\|Publication number in the designated or member state=KR20140045459\|Event publication date=2013-12-31\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=KR\|Event publication date=2017-07-05\|Event code=KR/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=KR\|MEMBER STATE LEGAL DETAILS FOR US20140120022\|Actual or expected expiration date=2020-11-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=US Corresponding appl: US14123987\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2012US-14123987\|Corresponding cc:\|Designated or member state=US Corresponding pat: US20140120022\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2014-05-01\|Publication number in the designated or member state=US20140120022\|Event publication date=2013-12-05\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=US\|Event publication date=2023-10-31\|Event code=US/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=US\|(CN103582611)\|LEGAL DETAILS FOR CN103582611\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201280027687\|Application date=2012-06-04\|Standardized application number=2012CN-80027687\|Event publication date=2014-02-12\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN103582611\|Publication stage code=A\|Publication date=2014-02-12\|Standardized publication number=CN103582611\|Event publication date=2014-02-12\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2014-06-04\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2017-03-08\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN103582611\|Publication stage code=B\|Publication date=2017-03-08\|Standardized publication number=CN103582611B\|Event publication date=2017-03-08\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2019-03-12\|Event code=CN/TR01\|Event group=Change of name or address Reassignment\|Transfer of patent right\|FORMER APPLICANT:Lafarge Holcim Ltd FORMER APPLICANT:LAFARGE SA APPLICANT:HOLCIM TECHNOLOGY LTD. APPLICANT:Lafarge Holcim Ltd\|Effective date of the event=2019-02-20\|Event publication date=2020-05-22\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee\|Effective date of the event=2019-06-04\|(HRP20180851)\|LEGAL DETAILS FOR HRP20180851\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=HR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=HR HRP20180851\|Application date=2012-06-04\|Standardized application number=2018HR-0000851\|Event publication date=2018-06-29\|Event code=HR/T1\|Event indicator=Pos\|Event group=Event indicating In Force\|Translation of the claims of an EP into Croatian\|Publication country=HR\|Publication number=HRP20180851\|Publication stage code=T1\|Publication date=2018-06-29\|Standardized publication number=HRP20180851\|Event publication date=2019-06-04\|Event code=HR/REG\|Event code=HR/PBON\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Reference to a national code\|LAPSE DUE TO NON-PAYMENT OF RENEWAL FEE\|Prestanak vrijednosti patenata zbog neodrzavanja\|Effective date of the event=2019-06-04\|(KR10-2014-0045459)\|LEGAL DETAILS FOR KR10-2014-0045459\|Actual or expected expiration date=2017-07-05\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=KR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=KR KR20137035129\|Application date=2012-06-04\|Standardized application number=2013KR-7035129\|Event publication date=2014-04-16\|Event code=KR/A\|Event group=Examination events\|Published application\|Publication country=KR\|Publication number=KR10-2014-0045459\|Publication stage code=A\|Publication date=2014-04-16\|Standardized publication number=KR20140045459\|Event publication date=2017-07-05\|Event code=KR/WITN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Withdrawal due to no request for examination\|(CA2838035)\|LEGAL DETAILS FOR CA2838035\|Actual or expected expiration date=2020-08-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2838035\|Application date=2012-06-04\|Standardized application number=2012CA-2838035\|Event publication date=2012-12-13\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2838035\|Publication stage code=A1\|Publication date=2012-12-13\|Standardized publication number=CA2838035\|Event publication date=2020-11-07\|Event code=CA/FZDE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Dead\|Effective date of the event=2020-08-31	(EP2718230)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP2532624)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP2532624)\|Extension States: ME, BA\|(WO2012/168176)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2012/168176)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2012/168176)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2012/168176)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2012/168176)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, RW, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KM, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PE, PG, PH, PL	(EP2718230)\|EP; AT\|(WO2012/168176)\|EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=9ru+nrv5joioDTVwA2ochGkyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP2718230&ekey=898&xpn=EP2718230&kind=B1	https://register.epo.org/application?number=EP12727348	https://permalink.orbit.com/RenderStaticFirstPage?XPN=92uohvSKJgbVNtz%252BuaPnF3fDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	EP	(WO2012/168176)\|FR\|(EP2532624)\|FR	(WO2012/168176)\|NAME=LAFARGE 61 rue des Belles Feuilles F-75116 Paris , COUNTRY=FR\|(EP2532624)\|NAME=LAFARGE 61, rue des Belles Feuilles , CITY=75116 Paris , COUNTRY=FR , REG=100163084	(EP2718230)\|AT\|(EP2718230)\|FR\|(EP2532624)\|FR\|\|(WO2012/168176)\|FR\|\|\|\|(CA2838035)\|CA	(EP2718230)\|NAME=Keschmann, Marc;Haffner und Keschmann Patentanwälte GmbH Schottengasse 3a , CITY=1014 Wien , COUNTRY=AT , REG=101393339\|(EP2718230)\|NAME=Mérigeault, Shona;Lafarge Département Propriété Industrielle (DPI) 95 Rue du Montmurier BP 9 , CITY=38291 Saint Quentin Fallavier Cedex , COUNTRY=FR , REG=101004378\|(EP2532624)\|NAME=Mérigeault, Shona;Lafarge Département Propriété Industrielle (DPI) 95 Rue du Montmurier BP 9 , CITY=38291 Saint Quentin Fallavier Cedex , COUNTRY=FR , REG=101004378\|(US9469546)\|NAME=Pillsbury Winthrop Shaw Pittman LLP\|(WO2012/168176)\|NAME=MERIGEAULT, Shona LAFARGE Département Propriété Intellectuelle (DPI) 95 rue du Montmurier - BP9 F-38291 Saint Quentin Fallavier Cedex , COUNTRY=FR\|(CN103582611)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314NAME=ZHU HUINING;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(CN103582611)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314NAME=ZHU HUINING;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(KR10-2014-0045459)\|NAME=KOREANA PATENT FIRM , REG=920011000013\|(CA2838035)\|NAME=NORTON ROSE FULBRIGHT CANADA LLP/S.E.N.C.R.L., S.R.L. , COUNTRY=CA	(EP2718230)\|FR; FR\|(EP2718230)\|FR; FR\|(EP2532624)\|FR; FR\|(US9469546)\|FR; FR\|(US20140120022)\|FR; FR\|(WO2012/168176)\|FR; FR\|(CN103582611)\|FR\|\|\|\|(CA2838035)\|FR; FR	(EP2718230)\|NAME=GARTNER, Ellis 42 rue Jean-Marc Bernard, CITY=F-69003 Lyon, COUNTRY=FR \|NAME=PISCH, Alexander Le Clos des Vignes 15 Traverse du Gamay, CITY=F-38090 Villefontaine, COUNTRY=FR\|(EP2718230)\|NAME=GARTNER, Ellis 42 rue Jean-Marc Bernard, CITY=F-69003 Lyon, COUNTRY=FR \|NAME=PISCH, Alexander Le Clos des Vignes 15 Traverse du Gamay, CITY=F-38090 Villefontaine, COUNTRY=FR\|(EP2532624)\|NAME=Gartner, Ellis 42 rue Jean-Marc Bernard, CITY=69003 LYON, COUNTRY=FR \|NAME=Pisch, Alexander Le clos des vignes 15 Traverse du Gamay, CITY=38090 Villefontaine, COUNTRY=FR\|(US9469546)\|NAME=Gartner Ellis, CITY=Lyons, COUNTRY=FR \|NAME=Pisch Alexander, CITY=Villefontaine, COUNTRY=FR\|(US20140120022)\|NAME=Gartner Ellis, CITY=Lyon, COUNTRY=FR \|NAME=Pisch Alexander, CITY=Villefontaine, COUNTRY=FR\|(WO2012/168176)\|NAME=GARTNER, Ellis 42 rue Jean-Marc Bernard F-69003 Lyon, COUNTRY=FR \|NAME=PISCH, Alexander Le Clos des Vignes 15 Traverse du Gamay F-38090 Villefontaine, COUNTRY=FR\|(CN103582611)\|NAME=E. Goldner Paris, FRA, CITY=Paris, STATE=Paris , COUNTRY=FR \|NAME=PISCH ALEXANDER\|(CN103582611)\|NAME=GARTNER ELLIS\|NAME=PISCH ALEXANDER\|(HRP20180851)\|NAME=Gartner, Ellis\|NAME=Pisch, Alexander\|(KR10-2014-0045459)\|NAME=GARTNER ELLIS\|NAME=PISCH ALEXANDER\|(CA2838035)\|NAME=GARTNER, ELLIS, COUNTRY=FR \|NAME=PISCH, ALEXANDER, COUNTRY=FR	(WO2012/168176)\|2\|(EP2718230)\|2\|(CN103582611)\|2\|(US9469546)\|2\|(KR10-2014-0045459)\|2\|(CA2838035)\|2\|(EP2532624)\|2	3	8			(EP2718230)\|WO2012/168176\|(US9469546)\|WO2012/168176\|(CN103582611)\|WO2012/168176\|(HRP20180851)\|WO2012/168176\|(KR10-2014-0045459)\|WO2012/168176\|(CA2838035)\|WO2012/168176	(HRP20180851)\|EP12727348	(EP2718230)\|Number of Claims: NCL=9\|\|(EP2532624)\|Number of Claims: NCL=10\|Primary examiner: Hartlieb, Ariane\|\|(US9469546)\|Number of Claims: NCL=5\|Number of Drawings: NDR=1\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=283\|Primary examiner: Berns Daniel\|Art Unit.: ART =1736\|\|(US20140120022)\|Number of Claims: NCL=12\|Number of Drawings: NDR=1\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Berns Daniel\|Art Unit.: ART =1736\|\|(WO2012/168176)\|Number of Claims: NCL=12\|Extended kind: EXTK=x\|\|(CN103582611)\|Number of Claims: NCL=8\|Gazette date: GAZDATE=2017-03-08\|Gazette number: GAZNUM=33-10\|Substantial examination effective date: 20140604 Examination duration: 33 months\|Number of Pages: NPAGES=13\|Primary examiner: Jiang Shuai\|Primary examiner: 江帅\|\|(CN103582611)\|Number of Claims: NCL=12\|Gazette date: GAZDATE=2014-02-12\|Gazette number: GAZNUM=30-07\|Substantial examination effective date: 20140604 Examination duration: 33 months\|Number of Pages: NPAGES=13\|Primary examiner: Jiang Shuai\|Primary examiner: 江帅\|\|(KR10-2014-0045459)\|Number of Claims: NCL=12\|Number of Pages: NPAGES=13\|\|(CA2838035)\|Number of Claims: NCL=10\|Number of Pages: NPAGES=18\|	(US9469546)\|Previous publication: US20140120022 A1 2014-05-01 [US20140120022]\|(CN103582611)\|Previous publication: CN103582611 A 2014-02-12 [CN103582611]	(EP2718230)\|ENGLISH (ENG)	(HRP20180851)\|Patent\|(EP2718230)\|Patent\|(CN103582611B)\|Patent\|(US9469546)\|Patent\|(US20140120022)\|Patent\|(EP2718230)\|Patent\|(KR20140045459)\|Patent\|(CN103582611)\|Patent\|(CA2838035)\|Patent\|(WO2012168176)\|Patent\|(EP2532624)\|Patent	Titre: (EP2718230)\|Process for the mineralization of carbon dioxide Résumé: (EP2718230)\|The invention provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form, or in the form of an alkali metal carbonate or bicarbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.	39	Abstract	gpt-4o-mini	yes	The process described involves the mineralization of CO₂ to form magnesium carbonate, which aligns with the goal of enhanced weathering and carbon sequestration using silicate minerals.
40	US63/256,986P\|US63/281,575P\|US63/298,412P	EP22157366	EP4166641	104628663	EP4166641 A1 2023-04-19 [EP4166641]	2021-10-18\|2021-11-19\|2022-01-11	2022-02-17	2023-04-19		(EP4166641)\|2023-10-20	(EP4166641)\|Systems and methods for processing olivine	(EP4166641)\|The present disclosure provides a system for processing olivine. The system may comprise a reactor for accelerating olivine weathering. The reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering.	PROJECT VESTA PBC	(EP4166641)\|Project Vesta, PBC ([US])	ROMANIELLO STEPHEN JUSTIN\|LEY BRIAN DAVID\|ANDREWS MARGARET GRACE\|WALWORTH NATHAN GERARD\|ISHOEY THOMAS\|GREEN TOM COXETER\|MONTSERRAT FRANCESC	(EP4166641)\|ROMANIELLO, Stephen Justin\|LEY, Brian David\|ANDREWS, Margaret Grace\|WALWORTH, Nathan Gerard\|ISHOEY, Thomas\|GREEN, Tom Coxeter\|MONTSERRAT, Francesc	(EP4166641)\|Hamer, Christopher K. ([GB])\|Reg. Nb: 100052783	(EP4166641)\|The systems and methods disclosed herein may enable efficient processing and deployment of olivine for purposes of CO2 capture in marine environments.\|The systems and methods of the present disclosure enable the acceleration of Earth's natural carbon removal method of rock weathering, through the extraction, processing (e.g., crushing and/or grinding), and transportation of volcanic mineral olivine to coastlines for dispersal or distribution.\|This may be a good reference to understand regulations for effluent from microbial processes.\|Although enhanced silicate weathering may be implemented in some instances, none of the prior work has [8] recognized and provided methods for the manufacture of engineered carbon-negative materials with specific suitable colors, grainsize, density, and reactivity required to meet specific regulatory, aesthetic, and engineering requirement for coastal engineering.\|In some embodiments, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process.\|Recognized herein are various limitations with current weathering methods, which may (i) involve long lead times and labor intensive procedures, (ii) impact ecological conditions (e.g., increasing water turbidity), and (iii) handling/processing of minerals that can pose additional ecological and health hazards via the possible ingestion, contact, or inhalation of fine grain of olivine mineral dust.\|	(EP4166641)\|1. A system for processing olivine, comprising:a reactor for accelerating olivine weathering, wherein the reactor comprises one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate said olivine weathering.\|7. A method, comprising: (a) generating one or more models for determining or predicting olivine dissolution, carbon sequestration, or one or more reaction fluxes associated with a dissolution of olivine in a target environment; (b) obtaining one or more sensor measurements at the target environment; (c) validating and/or updating the one or more models based on the one or more sensor measurements; and (d) using the one or more validated and/or updated models to determine or predict (i) olivine dissolution, (ii) carbon sequestration, and (iii) the one or more reaction fluxes in the target environment.\|	(EP4166641)\|The present application relates generally to using olivine to achieve enhanced weathering and increase CO2 uptake on accelerated timescales. In one aspect, the present disclosure provides systems and methods for accelerating weathering. In another aspect, the present disclosure provides a bioreactor configured to accelerate dissolution of olivine for weathering applications. In a further aspect, the present disclosure provides systems and methods for enhancing material properties of olivine. For example, the present disclosure provides a way to optimize the surface area effect of fine olivine grains by utilizing a binding process to bind or encapsulate the olivine fines into pellets of a larger effective grain size which can be more safely handled and distributed in the environment.\|The present disclosure provides a system for processing olivine.\|The present invention relates to a system for processing olivine. More specifically, the present invention relates to a system for processing olivine wherein the system comprises a reactor for accelerating olivine weathering, more particularly, the reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering.\|	(EP4166641)\|PROCESSING OLIVINE(100,6)\|OLIVINE DISSOLUTION(95,46)\|ENZYMATIC ACCELERANT(86,8)\|VOLCANIC MINERAL OLIVINE(76,2)\|TARGET ENVIRONMENT(73,7)\|OLIVINE(71,177)\|MODEL VALIDATION(71,1)\|ENHANCED SILICATE WEATHERING(65,1)\|ACCELERATED TIMESCALE(63,1)\|PELLETIZED OLIVINE AGGREGATE(60,2)\|OLIVINE GRAIN(57,16)\|MICROBE(56,4)\|OLIVINE DEPLOYMENT(55,2)\|DISSOLUTION ACCELERATOR(55,1)\|REACTOR(53,11)\|WEATHERING(52,2)\|FINE OLIVINE GRAIN(50,2)\|OLIVINE MINERAL DUST(48,1)\|OLIVINE FINE(47,3)\|MEDIATOR(46,8)\|MEASURING SENSOR(44,6)\|UPDATED MODEL(44,1)\|VOLCANIC MINERAL(41,3)\|ECOLOGICAL HARM(36,2)\|INGESTION(36,1)\|OLIVINE PARTICLE(35,6)\|OLIVINE MINERAL FINE(35,3)\|ECOLOGICAL CONDITION(35,1)\|FINE GRAIN(35,1)\|REACTION FLUX(32,3)\|INCREASE CO2 UPTAKE(31,1)\|OPERATING PARAMETER(31,1)\|OLIVINE SAND(30,20)\|COASTAL ENVIRONMENT(30,2)\|AQUATIC ENVIRONMENT(30,1)\|CARBON SEQUESTRATION(29,4)\|CO2 CAPTURE(28,10)\|PELLET(27,7)\|DISPERSION(27,1)\|INHALATION(27,1)\|LABOR INTENSIVE(27,1)\|CRUSHING(25,1)\|EFFLUENT(25,1)\|REACTIVITY(25,1)\|HEALTH HAZARD(24,1)\|MARINE LANDFILL CAP(23,6)\|OLIVINE DISSOLUTION KINETICS(23,3)\|COUNTERACTING OCEAN ACIDIFICATION COBENEFIT(23,1)\|BIOREACTOR(22,17)\|ACCELERATION(22,2)\|NATURAL CARBON REMOVAL(22,2)\|EQUIVALENTLY SIZED SOLID(21,2)\|COASTAL ENGINEERING(20,6)\|COASTLINE(20,5)\|INORGANIC FINE(20,3)\|REGULATION(20,2)\|MINERAL DUST(20,1)\|OLIVINE ENHANCING MATERIAL PROPERTY(20,1)\|TURBIDITY(19,4)\|MICROBIAL(19,1)\|TRANSPORTATION(18,5)\|INTERNAL POROSITY(18,2)\|CALCULATING ALKALINITY FLUX(17,3)\|COASTAL NOURISHMENT PROJECT(17,2)\|FUSION(16,2)\|MARINE ENVIRONMENT(16,2)\|SPLIT HULLED HOPPER BARGE(16,2)\|REMOVING CARBON(15,12)\|MINERAL(15,5)\|ENHANCED WEATHERING(15,4)\|PERMEABILITY(15,4)\|DREDGED SEDIMENT(15,3)\|BENTHIC INVERTEBRATE MEIOFAUNA(15,2)\|MARINE PHOTOSYNTHETIC MICROALGAE(15,1)\|OCEAN ACIDIFICATION MITIGATION(15,1)\|MICROBIAL BIOMASS(14,3)\|OCEAN ALKALINITY(14,3)\|OLIVINE DISSOLUTION BIOGEOCHEMICAL MODEL(14,1)\|SEA ACIDIFICATION COUNTERACTION(14,1)\|ROCK(13,11)\|CLAY MINERALOGY(13,2)\|CLAY SIMULTANEOUS PRECIPITATION(13,2)\|NONREACTIVE FEEDSTOCK(13,2)\|OCEAN DEACIDIFICATION(13,2)\|OLIVINE DISSOLUTION OPTIMIZATION(13,1)\|COASTAL CARBON CAPTURE(12,8)\|ACCELERATE OLIVINE(12,2)\|CR BIOACCUMULATION(12,2)\|HOPPER BARGE HULL(12,2)\|OLIVINE TRACER(12,2)\|ENGINEERED CARBON NEGATIVE MATERIAL(12,1)\|ENHANCING MATERIAL PROPERTY(12,1)\|TEMPORAL HETEROGENEITY EVALUATION(12,1)\|SHRINKING CORE MODEL(11,7)\|LARGE AGGREGATE(11,2)\|MICROBIAL PRODUCT(10,6)\|BIOMASS GENERATION(10,3)\|BEACH NOURISHMENT PROJECT(10,2)\|CALCULATING CO2 SEQUESTRATION(10,2)\|INTAKE SEAWATER(10,2)\|NI SPECIATION(10,2)\|OLIVINE REACTOR(10,2)\|PARTY ENTITY(10,2)\|PORE OVERVIEW(10,2)\|TOXIC POLLUTANT(10,2)\|BIOGENIC CALCIFICATION(10,1)\|CALCIFYING ORGANISM GROWTH(10,1)\|MARSH RESTORATION PROJECT(10,1)\|NEARBY COASTAL SHELF SEA(10,1)\|PHOTOSYNTHESIZING ALGAE(10,1)\|POREWATER GEOCHEMISTRY(10,1)\|SPATIOTEMPORAL HETEROGENEITY(10,1)\|SUCTION HOPPER DREDGE(10,1)\|SENSOR READING(9,5)\|CLAY FORMATION(9,4)\|CO2 TON(9,2)\|CLEAN UPLAND SAND(9,1)\|COASTAL COMMUNITY(9,1)\|FORSTERITE OLIVINE REACTION(9,1)\|FORSTERITE TON(9,1)\|ISOCAPNIC QUOTIENT(9,1)\|MARINE FOOD WEB CORNERSTONE(9,1)\|MITIGATING COASTAL EROSION(9,1)\|NET SILICATE DISSOLUTION(9,1)\|OCEAN ALKALINIZATION(9,1)\|OLIVINE ENHANCED DISSOLUTION(9,1)\|OLIVINE REDISTRIBUTION(9,1)\|OLIVINE SLOW DISSOLUTION(9,1)\|OLIVINE TRACKING(9,1)\|TURBIDITY PREDEPLOYMENT REDUCTION(9,1)\|ULTRAMAFIC INORGANIC MINERAL(9,1)\|SALINITY(8,5)\|GREEN HYDROGEN(8,4)\|MINERAL PROCESSING(8,3)\|TEMPORAL FACTOR(8,3)\|WEATHERING PRODUCT FORMATION(8,3)\|DEPLOYMENT SITE(8,2)\|DIATOM GROWTH(8,2)\|OLIVINE DISTRIBUTION(8,2)\|REGULAR CAP SAND(8,2)\|REGULATORY REQUIREMENT(8,2)\|SEAWATER AGE(8,2)\|WEATHERING(8,2)\|ALKALINITY EXPORT(8,1)\|ALKALINITY PROFILE NUMERIC SIMULATION(8,1)\|ALLOCHTHONOUS SAND(8,1)\|ANAEROBIC DIGESTION(8,1)\|ANAEROBIC RESPIRATION(8,1)\|APPLE IPHONE(8,1)\|ARTIFICIAL WEATHERING(8,1)\|ATTRIBUTE ENGINEERING(8,1)\|AUGMENT SEDIMENT(8,1)\|BEACH SEDIMENT(8,1)\|BENTHIC FLUX MEASUREMENT(8,1)\|CALCIFYING ORGANISM ABILITY(8,1)\|CALCULATING CO2 CAPTURE(8,1)\|CLAY PRECIPITATION(8,1)\|CRUSHED SANDSTONE(8,1)\|DIATOM ABUNDANCE(8,1)\|DISSOLUTION SIMULATION(8,1)\|EXTRACTING OLIVINE(8,1)\|GLOBAL LOGISTICS(8,1)\|GREEN VOLCANIC SILICATE MINERAL(8,1)\|HOPPER DREDGING(8,1)\|HYDROLOGIC SLURRY(8,1)\|INVOLUNTARY RESTRICTION(8,1)\|MARINE ECOSYSTEM HEALTH(8,1)\|MARITIME ASSET(8,1)\|MEASURING ALKALINITY FLUX(8,1)\|MITIGATE COASTAL EROSION(8,1)\|OLIVINE ABUNDANCE(8,1)\|OLIVINE DISSOLUTION ENVIRONMENT(8,1)\|REGIONAL OLIVINE DISSOLUTION RATE(8,1)\|SAND ENGINEERING REQUIREMENT(8,1)\|SEDIMENT DESTINATION(8,1)\|SUSTAINED MICROBIAL GROWTH(8,1)\|SUSTAINED SIDEROPHORE PRODUCTION(8,1)\|GRAIN SIZE(7,23)\|WAVE ENERGY(7,9)\|PLOT(7,7)\|COASTAL ENHANCED WEATHERING(7,5)\|BINDING AGENT(7,4)\|FLUID COMMUNICATION(7,4)\|MG2SIO(7,4)\|PHYSICAL COMPRESSION(7,2)\|PRIOR WORK(7,2)\|AGGREGATING RAW(7,1)\|ALK MOLE OLIVINE(7,1)\|ALKALINE SEAWATER(7,1)\|ALKALINITY CONSUMPTION(7,1)\|ARTIFICIALLY CREATED MINERAL(7,1)\|ATMOSPHERIC PCO(7,1)\|BENTHIC FLUX CHAMBER(7,1)\|BIOMASS SUSPENDED OLIVINE(7,1)\|CARBON CREDIT SALE VERIFICATION(7,1)\|CRUSHED LIMESTONE(7,1)\|DISSOLUTION BEHAVIOR(7,1)\|DISSOLVING OLIVINE(7,1)\|DREDGING MODIFICATION(7,1)\|EXTRACT OLIVINE(7,1)\|FLUX ACCURATE CALCULATION(7,1)\|INERT SAND(7,1)\|LADLE SLAG(7,1)\|LANDLINE NETWORK(7,1)\|MESOCOSM EXPERIMENT(7,1)\|METEOROLOGY IMPACT(7,1)\|MINERAL OLIVINE(7,1)\|NATIVE BEACH SAND(7,1)\|NATIVE SAND COLOR(7,1)\|NATURALLY CAPTURED CO2(7,1)\|NATURALLY OCCURRING NATIVE SEDIMENT(7,1)\|NATURALLY OCCURRING VOLCANIC MINERAL(7,1)\|NET CO2 FLUX(7,1)\|NONREACTIVE SEDIMENT COMPONENT(7,1)\|NONTOXIC CLAY(7,1)\|OCEAN ACIDITY(7,1)\|OCEAN SEDIMENT(7,1)\|OLIVINE DISSOLUTION RATE STUDY(7,1)\|OLIVINE FRACTION(7,1)\|OLIVINE MINERAL DISSOLUTION RATE(7,1)\|OLIVINE ROCK(7,1)\|OLIVINE TRANSPORT(7,1)\|OVERLYING SEAWATER(7,1)\|PERFECT SPHERE(7,1)\|POREWATER CHEMISTRY(7,1)\|PRECISE TIMESCALE(7,1)\|SAMSUNG TAB(7,1)\|SEA CO2 FLUX(7,1)\|SEAWATER CARBONATE(7,1)\|SEDIMENT HOPPER(7,1)\|SPARSE OBSERVATION(7,1)\|STABILIZING EARTH ATMOSPHERIC CO2(7,1)\|STRAIN OPTIMIZATION(7,1)\|COMPONENT REACTION(6,3)\|MACHINE EXECUTABLE CODE(6,3)\|PORE WATER PROFILE(6,3)\|PORTAL(6,3)\|PREDICTED RATE(6,3)\|ATMOSPHERIC CO2 UPTAKE(6,2)\|CIRCUM NEUTRAL PH(6,2)\|CO2 CONSUMPTION(6,2)\|COASTAL ECOSYSTEM(6,2)\|ECOLOGICAL RESPONSE(6,2)\|GAS CO2 FLUX(6,2)\|MAGNESIUM RELEASE(6,2)\|MICROMOL(6,2)\|MICROORGANISM(6,2)\|PARTICLE DISTRIBUTION(6,2)\|PHOTOSYNTHESIS(6,2)\|PROJECT SITE(6,2)\|WATER OXYGEN(6,2)\|ABSORB CO2(6,1)\|ACCURATE SIMULATION(6,1)\|ALKALINITY GENERATION(6,1)\|ALKALINITY MEASUREMENT(6,1)\|ALKALINITY SENSOR(6,1)\|ANALYTICAL MEASUREMENT(6,1)\|ATMOSPHERIC CO2 GIGATON(6,1)\|BEACH NOURISHMENT CYCLE(6,1)\|BIG FLUX(6,1)\|BIOMASS GROWTH(6,1)\|BLAST FURNACE SLAG(6,1)\|BOLSTERING LOCAL ECONOMY(6,1)\|CAPSIZING RISK(6,1)\|CARBON CREDIT VERIFIER(6,1)\|CARBONATE BEACH SAND(6,1)\|CARBONATE PRECIPITATION DISSOLUTION(6,1)\|COARSE PARTICLE(6,1)\|COASTAL ENGINEERING PROJECT(6,1)\|COMPUTER TANGIBLE MEMORY(6,1)\|CTDO SENSOR(6,1)\|CUSTOM STRAIN(6,1)\|DIURNAL FACTOR(6,1)\|DREDGING OPERATOR(6,1)\|ECOLOGICAL BENEFIT(6,1)\|ENHANCE OLIVINE(6,1)\|ENHANCED COASTAL EROSION(6,1)\|ENHANCING DISSOLUTION(6,1)\|EXCESS CO2 EMISSION(6,1)\|FE AVAILABILITY(6,1)\|FISHERY YIELD(6,1)\|GROUND OLIVINE(6,1)\|HUMAN CO2 EMISSION(6,1)\|IRON OXIDE(6,1)\|LEVER AGING NATURAL(6,1)\|MAGNESIUM RICH(6,1)\|MANAGEMENT SERVER(6,1)\|MARITIME EMISSIONS REDUCTION(6,1)\|MICROBIALLY MEDIATED TREATMENT(6,1)\|MINERAL REACTION(6,1)\|MONITOR OLIVINE(6,1)\|NATURAL SEAWATER(6,1)\|NET CAPTURE(6,1)\|OBJECTIVE CRITERIA(6,1)\|OLIVINE(6,1)\|OLIVINE DISSOLUTION SIGNAL(6,1)\|OLIVINE DISSOLUTION TEMPERATURE(6,1)\|OLIVINE GRAIN MOVEMENT(6,1)\|OLIVINE SPREADING LAYER(6,1)\|PROCESSED OLIVINE(6,1)\|PROTEINACEOUS COMPOUND(6,1)\|QUASI STEADY EQUILIBRIUM(6,1)\|RAW OLIVINE(6,1)\|RECIRCULATION LOOP(6,1)\|REVELLE FACTOR(6,1)\|SEAWATER RETURN(6,1)\|SEDIMENT MOTION(6,1)\|SEDIMENT TRANSPORT MODEL(6,1)\|SEDIMENT WATER ALKALINITY FLUX(6,1)\|SHALLOW SLOPE(6,1)\|SIDEROPHORE PRODUCTION YIELD(6,1)\|SILICATE BEACH SAND(6,1)\|SMALL OLIVINE GRAIN ENCAPSULATION(6,1)\|SOLUBLE BICARBONATE ION(6,1)\|STATIC DISSOLUTION(6,1)\|SULFIDE OXIDATION(6,1)\|TANGIBLE TRANSMISSION MEDIA(6,1)\|TARGET BEACH(6,1)\|WHITE OLIVINE(6,1)\|WIRED LINK(6,1)\|CPU(5,9)\|CO2 REACTIVE COMPONENT(5,5)\|SHIPPING(5,4)\|CORAL(5,3)\|SEAWATER PH(5,3)\|ALKALINITY FUNCTION(5,2)\|ATMOSPHERIC CARBON DIOXIDE(5,2)\|BASALT(5,2)\|BRUCITE(5,2)\|CARBON DIOXIDE EMISSION(5,2)\|CARBON NEGATIVE MATERIAL(5,2)\|CARBONATE PHASE(5,2)\|CHRYSOTILE(5,2)\|COMMUNICATION INTERFACE(5,2)\|EXTRANET(5,2)\|H4SIO4(5,2)\|INTRANET(5,2)\|ISOTOPIC TRACER(5,2)\|NATURALLY OCCURRING MINERAL(5,2)\|NUTRIENT(5,2)\|OLIVINE BREAKDOWN(5,2)\|REACTION TRANSPORT MODELING(5,2)\|SHOW DISSOLUTION(5,2)\|THRIVE(5,2)\|COMPUTER PROCESSOR(4,5)\|FLUORESCENT DYE(4,3)\|H2CO(4,3)\|MINING(4,3)\|QUARTZ(4,3)\|SHELL(4,3)\|SILICIC ACID(4,3)\|SPECTRAL PROPERTY(4,3)\|TEXTURE(4,3)\|TIDE(4,3)\|CLIENT(4,2)\|COASTAL PROTECTION(4,2)\|INTERNAL CHAMBER(4,2)\|ABUNDANT ION(4,1)\|ACCELERATE NATURAL CHEMICAL WEATHERING(4,1)\|AQUEOUS CO2 REMOVAL(4,1)\|BASELINE SITE(4,1)\|BICARBONATE PRODUCTION(4,1)\|BULK CARRIER DEPLOYMENT(4,1)\|BYPRODUCT(4,1)\|CAPTURE CO2(4,1)\|CARBON CAPTURE QUANTIFICATION(4,1)\|CARBON NEGATIVE SAND DISSOLUTION(4,1)\|CARBON REMOVAL VERIFICATION(4,1)\|CARBONATE PARAMETER(4,1)\|CARBONATE PRECIPITATION RATE(4,1)\|CLIMATE CHANGE MITIGATION LOCALE(4,1)\|COSTAL CARBON CAPTURE(4,1)\|DAMAGED AREA REGENERATION(4,1)\|DEPICTION(4,1)\|DIAGENESIS(4,1)\|DISSOLUTION MEASUREMENT(4,1)\|DISSOLUTION REACTION(4,1)\|DUAL BENEFIT(4,1)\|EXPOSED VOLCANIC ROCK(4,1)\|FINE FRACTION PARTICLE(4,1)\|FULL CARBONATE CHEMISTRY(4,1)\|GLOBAL MODEL(4,1)\|GLOBAL SCALE(4,1)\|GROUND NATURAL(4,1)\|INERT NATIVE(4,1)\|INORGANIC COATING(4,1)\|INORGANIC PARTICLE(4,1)\|INSOLUBLE IRON(4,1)\|LAND CONSTRUCTION(4,1)\|LARGE EFFECTIVE GRAIN SIZE(4,1)\|LIQUEFACTION REDUCTION(4,1)\|LIQUID ALKALINITY(4,1)\|MACHINE EXECUTABLE INSTRUCTION(4,1)\|MAGNESIUM ION(4,1)\|MEASURING TURBULENT ENERGY DISSIPATION(4,1)\|NATURAL BEACH SAND(4,1)\|NATURALLY OCCURRING OLIVINE(4,1)\|NATURALLY OCCURRING ROCK SEDIMENT(4,1)\|NEARBY COASTAL AREA(4,1)\|NITRATE SENSOR(4,1)\|NONTRANSITORY STORAGE(4,1)\|OCEAN REGION(4,1)\|OLIVINE CARBON CAPTURE REACTION(4,1)\|OLIVINE PROCESSING(4,1)\|OLIVINE THICK LAYER(4,1)\|OLIVINE VOLUME(4,1)\|REACTION NUMBER(4,1)\|REGULATORY PERMIT(4,1)\|SEAWATER MEDIUM(4,1)\|SEQUESTERING CARBON(4,1)\|SHALLOW MARINE ENVIRONMENT(4,1)\|SILICATE SENSOR(4,1)\|SIMULATION MODEL(4,1)\|SIMULTANEOUS BENEFIT(4,1)\|SOLUBLE MINERAL(4,1)\|SPECIALIZED SENSOR(4,1)\|STEEL FURNACE SLAG(4,1)\|SUBTROPICAL REGION(4,1)\|THERMODYNAMICS(4,1)\|TOTAL ALKALINITY SIMULTANEOUS MEASUREMENT(4,1)\|TRACK AIR SEAWATER(4,1)\|UNTRANSFORMED VOLUME(4,1)\|WIRELESS LINK(4,1)\|ACADEMIC(3,1)\|ACCEPTANCE(3,1)\|ACCOUNTING(3,1)\|AIR SEA CO2 EXCHANGE(3,1)\|AIR SEA EQUILIBRATION(3,1)\|ALKALINIZED SEAWATER ADDITION(3,1)\|ANDROID ENABLED(3,1)\|AQUACULTURE(3,1)\|ARAGONITE(3,1)\|ATMOSPHERIC GREENHOUSE GAS EMISSION(3,1)\|BIOLOGICAL ORGANISM(3,1)\|BIOTITE(3,1)\|BIOTURBATION(3,1)\|BLACKBERRY(3,1)\|CALCITE(3,1)\|CANDIDATE LOCATION(3,1)\|CARBON DIOXIDE CAPTURE(3,1)\|CARBON DIOXIDE IMPACT(3,1)\|CARBON DIOXIDE MOL(3,1)\|CARBON DISSOLUTION(3,1)\|CARBON NEGATIVE BATCH(3,1)\|CARBON REMOVAL PROJECT(3,1)\|CARBON REMOVING CAP BLEND(3,1)\|CELLULAR PROTEIN KEY COMPONENT(3,1)\|CHLORITE(3,1)\|CHLOROPHYL(3,1)\|CLIMATE CHANGE IMPACT(3,1)\|CO2 ABSORPTION RATE(3,1)\|CO2 OLIVINE RATIO(3,1)\|CO2 REACTIVE MINERAL COMPONENT(3,1)\|COASTAL ENGINEERING PRODUCT(3,1)\|COHESION(3,1)\|COLLISION(3,1)\|COMMUNICATION BUS(3,1)\|COMPUTER EXECUTABLE CODE(3,1)\|CONDUCTING CARBON NEUTRAL(3,1)\|CONSTRUCTION DEBRIS(3,1)\|CULTURING CONDITION(3,1)\|CUTTERHEAD DREDGING OPERATION(3,1)\|CYTOCHIP(3,1)\|DATABASE(3,1)\|DECADE(3,1)\|DEPTH MEASUREMENT(3,1)\|DISCRETE LOCATION(3,1)\|	(EP4166641)\|1. A system for processing olivine, comprising:\|a reactor for accelerating olivine weathering, wherein the reactor comprises one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate said olivine weathering.\|2. The system of claim 1, wherein the reactor is configured to adjust one or more operational parameters for processing olivine based on one or more sensors configured to measure carbon capture facilitated by said olivine weathering.\|3. The system of claim 1 or 2, wherein the olivine comprises pelletized olivine aggregates formed from olivine fines.\|4. The system of claim 3, wherein the olivine is prepared using [1] use of a binding agent, [2] via encapsulation of the olivine in one or more select materials or [3] via thermal fusion or physical compression of smaller olivine grains into larger aggregates.\|5. The system of claim 3 or 4, wherein the pellets are designed to either [i] remain substantially intact while maintaining improved surface area via internal porosity and permeability or [ii] degrade in a controlled fashion to release fine olivine fines to the environment in a prolonged controlled fashion.\|6. The system of any one of claims 3 to 5, wherein the preparation of the pellets allows olivine dissolution to occur substantially faster than would occur for equivalently sized solid pure olivine grains, improving the process of carbon capture, while minimizing the aesthetic, health, and ecological harm and challenges posed by working with and utilizing olivine mineral fines.\|7. A method, comprising:\| (a) generating one or more models for determining or predicting olivine dissolution, carbon sequestration, or one or more reaction fluxes associated with a dissolution of olivine in a target environment;\| (b) obtaining one or more sensor measurements at the target environment;\| (c) validating and/or updating the one or more models based on the one or more sensor measurements; and\| (d) using the one or more validated and/or updated models to determine or predict (i) olivine dissolution, (ii) carbon sequestration, and (iii) the one or more reaction fluxes in the target environment.\|8. The method of claim 7, wherein the target environment comprises a coastal or aquatic environment.\|9. The method of claim 7 or 8, further comprising providing olivine to the target environment.\|10. The method of claim 9, wherein the olivine is provided as part of a mixture comprising (i) the olivine and (ii) local beach sand at the target environment.	(EP4166641)\|CROSS REFERENCE\|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/256,986 filed on October 18, 2021, U.S. Provisional Patent Application No. 63/281,575 filed on November 19, 2021, and U.S. Provisional Patent Application No. 63/298,412 filed on January 11, 2022, each of which is incorporated herein by reference in its entirety for all purposes.\|BACKGROUND\|[0002] Enhanced weathering or accelerated weathering may be used to remove atmospheric carbon dioxide by leveraging natural or artificially created minerals that can absorb and transform carbon dioxide into other substances through chemical reactions that may occur in the presence of water (e.g., in the form of rain, groundwater or seawater).\|SUMMARY\|[0003] The present invention relates to a system for processing olivine. More specifically, the present invention relates to a system for processing olivine wherein the system comprises a reactor for accelerating olivine weathering, more particularly, the reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering. Enhanced weathering may be used in marine environments to increase ocean alkalinity and atmospheric CO2 uptake. In some cases, enhanced weather may involve adding processed minerals directly to the ocean or dumping the processed minerals on beaches where wave action can disperse the processed minerals into the target marine environment. Enhanced weathering may be used to reduce CO2 levels in the atmosphere while also counteracting ocean acidification.\|[0004] Recognized herein are various limitations with current weathering methods, which may (i) involve long lead times and labor intensive procedures, (ii) impact ecological conditions (e.g., increasing water turbidity), and (iii) handling/processing of minerals that can pose additional ecological and health hazards via the possible ingestion, contact, or inhalation of fine grain of olivine mineral dust.\|[0005] The present application relates generally to using olivine to achieve enhanced weathering and increase CO2 uptake on accelerated timescales. In one aspect, the present disclosure provides systems and methods for accelerating weathering. In another aspect, the present disclosure provides a bioreactor configured to accelerate dissolution of olivine for weathering applications. In a further aspect, the present disclosure provides systems and methods for enhancing material properties of olivine. For example, the present disclosure provides a way to optimize the surface area effect of fine olivine grains by utilizing a binding process to bind or encapsulate the olivine fines into pellets of a larger effective grain size which can be more safely handled and distributed in the environment. The ability to tailor the design of pellets composed of olivine mineral fines by using different binding agents or encapsulation processes provides the ability to tailor and control the porosity, permeability, and degradation characteristics of the olivine-containing pellets, controlling their dissolution behavior in the environment. The systems and methods disclosed herein may enable efficient processing and deployment of olivine for purposes of CO2 capture in marine environments.\|[0006] In some embodiments, pelletized olivine aggregates formed from olivine fines may be prepared through a number of processes disclosed herein including [1] the use of a binding agent (such as but not limited to clay, polysaccharides, proteinaceous compounds, resin, plastic, glass, etc.) [2] via encapsulation of smaller olivine grains with said binding agent or other similar materials or [3] via the thermal fusion or physical compression of smaller olivine grains into larger aggregates.\|[0007] In some embodiments, the pellets may be designed to either [4] remain substantially intact while maintaining improved surface area via internal porosity and permeability or [5] degrade in a controlled fashion to release fine olivine fines to the environment in a prolonged controlled fashion. In some cases, [6] the preparation of such pellets may allow olivine dissolution to occur substantially faster than would occur for equivalently sized solid pure olivine grains, thereby improving the process of carbon capture while minimizing the aesthetic, health, and ecological harm and challenges posed by working with and utilizing olivine mineral fines.\|[0008] Another aspect of the present disclosure provides a non-transitory computer readable medium comprising machine executable code that, upon execution by one or more computer processors, implements any of the methods above or elsewhere herein.\|[0009] Another aspect of the present disclosure provides a system comprising one or more computer processors and computer memory coupled thereto. The computer memory comprises machine executable code that, upon execution by the one or more computer processors, implements any of the methods above or elsewhere herein.\|[0010] Additional aspects and advantages of the present disclosure will become readily apparent to those skilled in this art from the following detailed description, wherein only illustrative embodiments of the present disclosure are shown and described. As will be realized, the present disclosure is capable of other and different embodiments, and its several details are capable of modifications in various obvious respects, all without departing from the disclosure. Accordingly, the drawings and description are to be regarded as illustrative in nature, and not as restrictive.\|INCORPORATION BY REFERENCE\|[0011] All publications, patents, and patent applications mentioned in this specification are herein incorporated by reference to the same extent as if each individual publication, patent, or patent application was specifically and individually indicated to be incorporated by reference. To the extent publications and patents or patent applications incorporated by reference contradict the disclosure contained in the specification, the specification is intended to supersede and/or take precedence over any such contradictory material.\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0012] The novel features of the invention are set forth with particularity in the appended claims. A better understanding of the features and advantages of the present invention will be obtained by reference to the following detailed description that sets forth illustrative embodiments, in which the principles of the invention are utilized, and the accompanying drawings (also "Figure" and "FIG." herein), of which:\| FIG. 1 schematically illustrates the long-term carbonate-silicate cycle, in accordance with some embodiments.\| FIG. 2 schematically illustrates the chemical processes by which olivine can be used to capture and sequester CO2, in accordance with some embodiments.\| FIG. 3 schematically illustrates the chemical reactions that enable CO2 capture and sequestration using olivine, in accordance with some embodiments.\| FIG. 4 schematically illustrates olivine and mixtures of sand and olivine, in accordance with some embodiments.\| FIG. 5 schematically illustrates one exemplary method for using olivine to remove atmospheric CO2 and increase ocean alkalinity, in accordance with some embodiments.\| FIG. 6 schematically illustrates the use of wave energy to cause sand grains and/or olivine grains to collide and break into smaller pieces, thereby facilitating the dissolution of olivine, in accordance with some embodiments.\| FIG. 7 schematically illustrates an example of how the oceans can be used for natural carbon storage, in accordance with some embodiments.\| FIG. 8 schematically illustrates an example of a bioreactor, in accordance with some embodiments.\| FIG. 9 schematically illustrates an example of a system for deploying olivine for coastal nourishment, in accordance with some embodiments.\| FIG. 10 schematically illustrates a computer system that is programmed or otherwise configured to implement methods provided herein.\| FIG. 11 schematically illustrates an exemplary reactor configured to intake seawater that may be mixed with olivine and microbial biomass to generate alkalinity.\| FIG. 12 schematically illustrates an exemplary protocol for measuring, recording, and verifying (MRV) carbon removal, in accordance with some embodiments.\| FIGs. 13 - 14 schematically illustrate a chemical reaction by which coastal carbon capture occurs when olivine is introduced to a target site, in accordance with some embodiments.\| FIGs. 15 - 20 schematically illustrate an environment in which olivine can be introduced for costal carbon capture, in accordance with some embodiments.\| FIGs. 21A and 21B schematically illustrates a plot of concentration of an alkaline material in a flux chamber as a function of time, in accordance with some embodiments.\| FIG. 22 schematically illustrates an overview of the porewater method, in accordance with some embodiments.\| FIG. 23 schematically illustrates a shrinking core model, in accordance with some embodiments.\| FIG. 24 schematically illustrates dissolution rates for olivine having various grain sizes, in accordance with some embodiments.\| FIG. 25 schematically illustrates an exemplary modeling approach for particle distribution, in accordance with some embodiments.\| FIG. 26 schematically illustrates dissolution rates for different mixtures of olivine having different mean grain sizes, in accordance with some embodiments.\| FIG. 27 schematically illustrates the impact of temperature and pH on olivine half-life, in accordance with some embodiments.\| FIG. 28 schematically illustrates examples of temporal factors and spatial factors that can vary for coastal ecosystems, in accordance with some embodiments.\| FIG. 29 schematically illustrates plots of the temporal heterogeneity of various characteristics for a target site, in accordance with some embodiments.\| FIGs. 30 - 32 schematically illustrate examples of factors to consider when calculating alkalinity fluxes, in accordance with some embodiments.\| FIG. 33 shows a summary of various approaches for measuring, recording, and verifying carbon capture and olivine dissolution at different scales of cost and complexity, in accordance with some embodiments.\| FIG. 34 schematically illustrates various reaction-transport modeling studies that may be used to simulate sediment porewater profiles, solid-phase chemistry, and benthic fluxes, in accordance with some embodiments.\| FIGs. 35 - 36 schematically illustrate various examples of sensors that can be used for measuring, recording, and verifying carbon capture and/or olivine dissolution, in accordance with some embodiments.\| FIGs. 37 - 38 schematically illustrate reactions that may occur when olivine sand is introduced to beaches, in accordance with some embodiments.\| FIG. 39 schematically illustrates an approach to calculating CO2 sequestration from alkalinity flux based on an expression of how water DIC storage changes as a function of increasing alkalinity, in accordance with some embodiments.\| FIG. 40 schematically illustrates a plot showing seawater age and the depth below sea water level of the Atlantic Ocean as a function of latitude (degrees North), in accordance with some embodiments.\| FIG. 41 schematically illustrates an exemplary coastal enhanced weathering (CEW) life cycle analysis, in accordance with some embodiments.\| FIG. 42 schematically illustrates an example of a carbon payback period that can be realized using the methods and systems disclosed herein, in accordance with some embodiments.\| FIG. 43 schematically illustrates various plots showing exemplary olivine dissolution kinetics for olivine particles having different grain sizes, in accordance with some embodiments.\| FIG. 44 schematically illustrates the effects of secondary carbonate precipitation on CO2 capture efficiency, in accordance with some embodiments.\| FIG. 45 schematically illustrates the effects of secondary clay formation on CO2 capture efficiency, in accordance with some embodiments.\|DETAILED DESCRIPTION\|[0013] While various embodiments of the invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. Numerous variations, changes, and substitutions may occur to those skilled in the art without departing from the invention. It should be understood that various alternatives to the embodiments of the invention described herein may be employed.\|[0014] Whenever the term "at least," "greater than," or "greater than or equal to" precedes the first numerical value in a series of two or more numerical values, the term "at least," "greater than" or "greater than or equal to" applies to each of the numerical values in that series of numerical values. For example, greater than or equal to 1, 2, or 3 is equivalent to greater than or equal to 1, greater than or equal to 2, or greater than or equal to 3.\|[0015] Whenever the term "no more than," "less than," or "less than or equal to" precedes the first numerical value in a series of two or more numerical values, the term "no more than," "less than," or "less than or equal to" applies to each of the numerical values in that series of numerical values. For example, less than or equal to 3, 2, or 1 is equivalent to less than or equal to 3, less than or equal to 2, or less than or equal to 1.\|[0016] The term "real time" or "real-time," as used interchangeably herein, generally refers to an event (e.g., an operation, a process, a method, a technique, a computation, a calculation, an analysis, a visualization, an optimization, etc.) that is performed using recently obtained (e.g., collected or received) data. In some cases, a real time event may be performed almost immediately or within a short enough time span, such as within at least 0.0001 millisecond (ms), 0.0005 ms, 0.001 ms, 0.005 ms, 0.01 ms, 0.05 ms, 0.1 ms, 0.5 ms, 1 ms, 5 ms, 0.01 seconds, 0.05 seconds, 0.1 seconds, 0.5 seconds, 1 second, or more. In some cases, a real time event may be performed almost immediately or within a short enough time span, such as within at most 1 second, 0.5 seconds, 0.1 seconds, 0.05 seconds, 0.01 seconds, 5 ms, 1 ms, 0.5 ms, 0.1 ms, 0.05 ms, 0.01 ms, 0.005 ms, 0.001 ms, 0.0005 ms, 0.0001 ms, or less.\|Overview\|[0017] To avoid the worst effects of climate change, we must rapidly remove billions of tons of CO2 from the atmosphere. There are currently no proven methods for doing so. There is an urgent need to identify carbon removal methods that are permanent, scalable, and economical.\|[0018] The earth's natural long-term carbonate-silicate cycle is how our planet has naturally captured CO2 over thousands of years. Over millennia, rain falling on exposed volcanic rock causes it to weather, which removes CO2 from the atmosphere as bicarbonate dissolved in water. This water flows to the oceans, where marine calcifying organisms incorporate the CO2 into their shells and skeletons. When they die, they form ocean sediment, ultimately becoming limestone.\|[0019] The systems and methods of the present disclosure enable the acceleration of Earth's natural carbon removal method of rock weathering, through the extraction, processing (e.g., crushing and/or grinding), and transportation of volcanic mineral olivine to coastlines for dispersal or distribution. In some embodiments, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process. In other embodiments, a bioreactor may be used to enhance and facilitate olivine dissolution. In either case, carbon dioxide may be removed from the atmosphere as the olivine breaks down.\|[0020] Coastal Carbon Capture, also known as Coastal Enhanced Weathering, can be categorized as a negative emission technology (NET) that removes and stores CO2 on long timescales (tens to hundreds of thousands of years). The process aims to accelerate the natural chemical weathering of the mineral olivine by spreading large amounts of ground olivine-containing rock onto coastlines or bioreactors positioned on or near such coastlines, where it can dissolve in seawater, thereby increasing the rate of CO2 absorption by the ocean.\|[0021] The present disclosure provides systems and methods for accelerating the Earth's natural carbon removal method of rock weathering, by extracting the volcanic mineral olivine, grinding it into sand, and deploying it on coastlines or in bioreactors located on said coastlines. There, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process. Carbon dioxide is removed from the atmosphere as the olivine breaks down.\|[0022] FIG. 1 illustrates the long-term carbonate-silicate cycle. The illustrated reaction is the foundation of the Long-Term Inorganic Carbon Cycle, which has been occurring for billions of years, stabilizing Earth's atmospheric CO2 concentrations, and in turn enabling life to thrive. In fact, carbon dioxide removal (CDR) through natural rock weathering consumes ~1 gigaton of CO2 every year. Natural CO2 removal through rock weathering may be achieved through the following steps:\| 1. Rain falls on volcanic rocks, slowly dissolving them.\| 2. Carbonic acid dissolved in the rainwater reacts with silicate from the rocks, shifting the equilibrium from carbonic acid to bicarbonate.\| 3. This bicarbonate flows to the ocean.\| 4. Marine organisms use this as calcium carbonate in their shells and skeletons; when they die this becomes limestone.\| 5. Limestone formed at the ocean floor eventually subducts, locking up the carbon for millions of years.\|[0023] FIG. 2 illustrates the chemical processes that are enabled by olivine to perform CO2 capture and sequestration. FIG. 3 illustrates the chemical reactions that enable CO2 capture and sequestration using olivine. As the olivine dissolves, its products are magnesium ions (the second most abundant ion in the ocean behind sodium), silicate (used by diatoms to build their skeletons) and dissolved carbon. Referring to FIG. 2 and FIG. 3, when olivine dissolves in water, it drives the illustrated reaction, thus increasing CO2 uptake, raising pH, and generating alkalinity. As a result, this process has the potential co-benefit of counteracting ocean acidification. Ocean acidification is the process by which increasing atmospheric CO2 dissolves in seawater, which reduces pH (increasing acidity) (upper reaction in diagram below). This reduces the ability of calcifying organisms like corals to grow and produce exoskeletons, or shells. As shown in FIG. 2 and FIG. 3, dissolving olivine in water sequesters hydrogen ions into dissolved silicate (H4SiO4), a molecule that can be used by diatoms, an important photosynthesizing algae that fixes carbon dioxide and forms the base of food web.\|[0024] Unfortunately, natural chemical weathering happens too slowly to balance human CO2 emissions and is already accounted for in Earth's present-day carbon budget. The systems and methods disclosed herein can be deployed and implemented to accelerate this natural process to remove at least a gigaton of atmospheric CO2 per year on a global scale.\|Accelerating a Natural Process\|[0025] Coastal Carbon Capture can be used to accelerate Earth's natural CO2 removal process. At current rates, the natural process of rock weathering through rainfall needs to be sped up by at least 100 times to absorb the CO2 emitted by human activity. Coastal Carbon Capture (CCC) can accelerate the process by using wave energy and/or bioreactors to break down olivine. The rock containing the olivine may be placed in high-energy coastal environments, where wave energy mechanically activates the rock, causing collisions which remove the silica coating and efficiently grind the olivine down. The olivine sand then dissolves in the water at a rate orders of magnitude faster than in the geological process.\|[0026] Coastal Carbon Capture may comprise the following steps:\| 1. Extract olivine and efficiently grind it. Olivine is a green volcanic silicate mineral. It is highly abundant and found near the surface all over the world. Olivine rocks can be efficiently crushed to sand and gravel grain sizes.\| 2. Transport olivine to a nearby coastal area. The olivine sand may be transported (e.g., by rail, ship, or truck) to a nearby coastal shelf sea. There, it may be spread in a thin layer.\| 3. Wave energy may accelerate CO2 removal. Wave energy and currents may further grind down the olivine. Grain-on-grain collisions can cause fine fraction particles (< 10 microns) to form, which then weather very rapidly. The olivine may consequently dissolve in the water rapidly, accelerating the reaction which removes CO2 from the ocean/atmosphere.\|[0027] FIG. 5 illustrates one exemplary method for using olivine to remove atmospheric CO2 and increase ocean alkalinity. As shown in FIG. 6, wave energy may cause sand grains and/or olivine grains to collide and break into smaller pieces, thereby facilitating the dissolution of olivine.\|Olivine\|[0028] Olivine is a common, naturally occurring volcanic mineral, with physical properties similar to quartz. Olivine may be 23% denser than quartz sand (1.43 tons/cy). Olivine sand is a clean upland sand that is 25% denser than silicate sand, and that can be artificially milled to match native grain size. Darker and lighter olivine sources allow for color matching to the native sand color.\|[0029] Olivine can be processed to yield fine olivine grains with increased surface area exposure, which can speed up dissolution and the CO2 capture process. The olivine dissolution and CO2 capture process can also be accelerated by (i) using reactive and soluble minerals, (ii) increasing an amount of surface area of the olivine grains that is exposed to a solvent (e.g., water or seawater), (iii) enhancing fluid-mineral interactions, and/or (iv) reducing or eliminating secondary mineral coatings or the formation of secondary weathering products (e.g., precipitation of secondary clays and carbonate phases).\|[0030] Once deployed on a beach, olivine can capture 20 times more carbon than is emitted in the mining, milling, shipping, and beach nourishment operation. 1 ton of olivine sand can capture up to 1.25 tons of carbon in ideal situations. Since it takes olivine several decades to weather, it will provide effective coastal protection during long-term beach nourishment cycles.\|[0031] One type of olivine may be white olivine, or Forsterite (Mg2SiO4). This is a magnesium rich form of olivine, known as Forsterite (Mg2SiO4). Weathering 1 ton of olivine can remove up to 1.25 tons of CO2 from the atmosphere.\|[0032] FIG. 4 illustrates olivine and mixtures of sand and olivine. In some cases, the olivine may be mixed with natural beach sand before the olivine is deployed at a target site. The mixture comprising the olivine may comprise at least about 5%, 10%, 15%, 20%, 25%, or 30% olivine by weight or volume. In some cases, the mixture may comprise more than 30% olivine by weight or volume. In some cases, the mixture may comprise less than 5% olivine by weight or volume. In some cases, the mixture may comprise between about 5% and about 30% olivine by weight or volume.\|[0033] Beneficial applications of olivine include, for example, Marsh Restoration, Coastal Engineering/Hazard Mitigation, and CO2 Capture. As described above, olivine sand can react with water and CO2. CO2 may dissolve in water to form carbonic acid. Olivine dissolution may consume the carbonic acid to yield soluble bicarbonate ion (baking soda). This can: Lower atmospheric CO2, Neutralize ocean acidification, and Support the growth of calcifying organisms (Corals, etc).\|[0034] In some cases, olivine sand may be provided to municipalities to augment the sediment used in beach nourishment projects. As the sand weathers, it captures carbon. The sand and its placement are paid for by carbon credits. Therefore, the greater the percentage of olivine sand mixed into the native sand, the cheaper the beach nourishment project. A 10% mix would mean a -10% decrease in sand cost. Through the use of olivine sand, beach nourishment can play a critical role in reversing climate change and ocean acidification if the right mix of native and olivine sand is used. At scale, over a billion tons of CO2 could be removed from the atmosphere every year.\|[0035] Using wave action to break down the olivine is critical to the life cycle. Past analyses have shown that grinding the olivine down to <100µm size is highly energy-intensive. However, grinding the olivine down to >300µm gravel requires far less energy. Using the natural, free energy of water movement to break the olivine down further reduces the milling and grinding energy to a small proportion of the total.\|[0036] Co-Benefits of the methods described herein include, for example: reduction in Ocean Acidification (OA). Ocean acidification has been shown to damage marine ecosystems. Olivine increases local pH levels, potentially mitigating the adverse effects of OA on marine ecosystems. This could potentially improve aquaculture and fishery yields, bolstering local economies at deployment sites as well as reversing damage to marine ecosystems. FIG. 7 illustrates an example of how the oceans can be used for natural carbon storage. Excess CO2 emissions may increase ocean acidity. The systems and methods of the present disclosure may be implemented to reduce acidity and help the oceans safely store more CO2 as bicarbonate.\|[0037] Co-Benefits of the methods described herein may also include, for example: support for diatom growth. Diatoms, marine photosynthetic microalgae, are a cornerstone of marine food webs and capture CO2 through photosynthesis, creating 40% of oxygen on Earth. Diatom abundance has decreased as CO2 has risen, partly due to decreasing concentrations of silicate in the ocean due to damming of rivers limiting sediment flow. Since olivine is primarily magnesium silicate, the increase in silicate concentrations from olivine dissolution may lead to diatom growth. Increases in diatoms would increase the health of marine ecosystems and support photosynthetic carbon capture. Other co-benefits can include, for example, supporting coastal communities facing enhanced coastal erosion and sea level rise by supplying a low-cost source of sediment (which may be paid for using carbon credits).\|Mechanics of Weathering\|[0038] In some cases, grain-on-grain collisions may rapidly break down the olivine. Olivine grains may be reduced in size due to mechanical activation. In some cases, the motion of the water in which the olivine is provided may cause surface abrasions. In some cases, the surface of the olivine grains may be mechanically activated to enable and/or enhance CO2 uptake and de-acidification.\|Sensors\|[0039] In some cases, one or more sensors may be used to track, monitor, and quantify olivine dissolution, CO2 uptake, and ocean de-acidification. The measurements obtained using the sensors may be used to adjust the preparation or processing of the olivine, the optimal properties of the olivine, the location in which the olivine is introduced, the rate at which the olivine is introduced, a method by which the olivine is distributed, or a configuration/form in which the olivine is distributed.\|[0040] In some cases, the one or more sensors may be used to monitor and track: Olivine Dissolution Rates (Porewater Geochemistry, Benthic Flux Measurements), Impacts on Water Chemistry, Ecological Response, Fate, Transport and Bioaccumulation of Cr and Ni, and/or Formation of Secondary Weathering Products (Chrysotile, Carbonates, Clays). In some cases, an isotopic tracer along with [Si] and [ALK] measurements may be used to track olivine dissolution and simultaneous precipitation of secondary clays and carbonate phases. The sensors may also be used to track olivine grains over time [ie physical tracking of olivine using dyes / tracers, etc.].\|Reaction-Transport Modeling\|[0041] In some cases, simulation models may be used to optimize the preparation or processing of the olivine, the properties of the olivine, the location in which the olivine is introduced, the rate at which the olivine is introduced, a method by which the olivine is distributed, or a configuration/form in which the olivine is distributed. The models may be configured to simulate sediment porewater profiles, Water column and Porewater Chemistry (e.g., pCO2, DIC, pH, DO, TA, Nutrients, Metals, DOC), solid-phase chemistry and benthic fluxes, Secondary Clay Mineralogy, and Cr and Ni speciation and cycling. In some cases, the models may be used for simulation of the effects of spreading layers of olivine sand of varying thicknesses on a target beach sediment with one or more known biological, chemical, or ecological properties or characteristics.\|[0042] In some cases, the models may be used simulate or predict Olivine Dissolution Rates, study the impacts of Temperature of Olivine Dissolution & Respiration, track impacts on seawater pH, track Air-Sea Water Gas CO2 Fluxes, monitor and evaluate fate and transport of Cr and Ni, assess the impacts on benthic invertebrates/meiofauna, track sediment characteristics (e.g., changes in mineralogy, formation of secondary carbonate/clays), monitor the impacts of Meteorology and Hydrology (e.g., temperature, wind speed/direction, precipitation, salinity, turbidity, current), or simulate Physical Sediment Transport and/or Olivine Redistribution.\|Method of Removing Atmospheric Carbon\|[0043] [1] In one aspect, the present disclosure provides a method for removing atmospheric carbon using olivine dissolution technologies. The method may be implemented using natural wave energy (i.e., in situ coastal enhanced weathering (CEW)) and/or applied energy (i.e., closed-system artificial weathering of olivine in a man-made reactor or a sand pit resulting from coastal nourishment projects or dredging).\|Bioreactor\|[0044] In another aspect, the present disclosure provides systems and methods to accelerate olivine dissolution reactions in a bioreactor. The bioreactor may comprise one or more internal chambers for housing or storing olivine for any amount of time. The bioreactor may comprise one or more openings or inlets for receiving olivine. The olivine may comprise pure olivine or a mixture of olivine and sand or other elements or materials. The olivine may be unprocessed. Alternatively, the olivine may be processed or pre-processed (e.g., by grinding).\|[0045] In some cases, the bioreactor may comprise one or more mechanical components for mechanical weathering of the olivine. The mechanical weather may cause grain-on-grain collisions that may rapidly break down the olivine. Olivine grains may be reduced in size due to mechanical activation. In some cases, the bioreactor may be in fluid communication with water. In some cases, the bioreactor may comprise an internal chamber for housing the water and/or the olivine. The motion of the water in which the olivine is introduced may cause surface abrasions. In some cases, the surface of the olivine grains may be mechanically activated to enable and/or enhance CO2 uptake and ocean de-acidification.\|[0046] In some cases, the mechanical components may comprise one or more gears or actuators for inducing a motion that cause mechanical weathering of the olivine. The motion may be a linear motion, or a rotational motion, or any combination thereof.\|[0047] In some cases, the bioreactor may comprise a chamber for housing one or more microbial products or other biological mediators and/or enzymatic accelerants that can help to further break down the olivine. The chamber housing the microbial products may be in fluid communication with (i) the chamber housing the olivine, (ii) the chamber that is in fluid communication with the ocean water, or both (i) and (ii).\|[0048] FIG. 8 schematically illustrates an example of a bioreactor 800. The bioreactor 800 may be configured to receive olivine, which olivine may or may not be pre-processed (e.g., by grinding or crushing). The olivine may be stored within a first chamber 810 of the bioreactor 800 for further processing. In some cases, the bioreactor 800 may comprise a second chamber 820 configured to house one or more microbial products or other biological mediators and/or enzymatic accelerants that can help to further break down the olivine. In some cases, the bioreactor 800 may comprise a third chamber 830. The third chamber 830 may comprise a reaction chamber in fluid communication with the first chamber 810 and the second chamber 820. The third chamber 830 may be used to break down the olivine using the microbial products or other biological mediators and/or enzymatic accelerants. Once broken down, the processed olivine may be provided to a target region external to the bioreactor 800 to facilitate CO2 capture and sequestration.\|Microbes\|[0049] [2] In another aspect, the present disclosure provides a method for enhanced dissolution of olivine through (1) microbial products or other biological mediators and (2) enzymatic accelerants. The method may comprise enhancing dissolution of olivine in an olivine reactor or sand pit resulting from coastal nourishment projects or dredging through: microbial products or other biological mediators; and enzymatic accelerants.\|[0050] In another aspect, the present disclosure provides systems and methods for olivine dissolution by microorganisms, biological organisms, and/or biological mechanisms. The dissolution of olivine in water may consume protons and increase alkalinity, thereby removing dissolved aqueous CO2. This aqueous CO2 removal may induce additional CO2 to be taken up from the atmosphere and subsequently converted to bicarbonate, carbonate, and/or solid-phase carbonate minerals, thereby sequestering carbon for long time periods [1]. Scaling and accelerating this process has the potential to mitigate climate change and ocean acidification.\|[0051] In some cases, the reactors disclosed herein may be designed to grow particular microbial strains in an aqueous medium in order to induce metabolic states that can accelerate olivine dissolution. In circum-neutral pH naturally oxygenated waters, ferric iron (Fe2+) contained within olivine may be rapidly oxidized to ferrous iron (Fe3+) by oxygen even in the absence of microbial activity [2]. This oxidized iron can form a surface layer of Fe-oxyhydroxides on the mineral surface of olivine which can shield portions of its total surface area from contact with solution [3]. These Fe-oxyhydroxide surface coatings can, in some cases, impede olivine dissolution [4].\|[0052] For the vast majority of organisms, Fe is a required nutrient and a key component of many cellular proteins. However, most Fe in naturally oxygenated waters at circum-neutral pH is insoluble and typically complexed to particles. Certain microorganisms can produce organic compounds known as siderophores to mobilize and acquire insoluble iron on mineral surfaces [2], which can concurrently increase olivine mineral dissolution rates [3]. However, the production of siderophores may be regulated by Fe availability to the cells. As more Fe is acquired by the cells (i.e. the less iron-limited they are), siderophore production may decrease, which may slow dissolution rates. Hence, in order to sustain and scale siderophore production over extended time periods in large reactors, numerous interacting factors may be optimized:\| 1. The most optimized biological strains (these may be identified through a series of experiments, and in some cases, custom strains may be generated either through directed evolution or genetic editing).\| 2. The optimal ratios of microbial to siderophore concentrations given certain growth conditions.\| 3. Olivine dissolution optimization as a function of particle size/surface area and flow rate from biomass generation.\| 4. Optimized long-term growth conditions for sustained siderophore production.\| 5. Optimized reactor design series including appropriate materials to avoid silicate and trace metal contamination.\| 6. Development of mathematical model to optimize siderophore production yield, biomass generation, and olivine dissolution.\| 7. Development of appropriate parameters to track to feed into the model.\| 8. Development of any treatment of seawater effluent prior to returning to the ocean.\| 9. Development of a model that calculates CO2 sequestration from the addition of alkalinized seawater to the local ocean region.\|System Design\|[0053] Referring to FIG. 11, the illustrated reactor may be configured to intake seawater that may be mixed with olivine and microbial biomass to generate alkalinity. Depending on the source, seawater may have to be pretreated prior to reacting with olivine. This reaction may also result in trace metals, microbial biomass, and other reaction products mixing in with the seawater medium. In order to sequester carbon at scale, this alkaline seawater may be returned to the ocean to induce atmospheric CO2 uptake. Importantly, the return of this seawater containing the certain constituents must meet local regulations. Another microbially-mediated treatment process that returns effluent to the environment may involve anaerobic digestion. This may be a good reference to understand regulations for effluent from microbial processes.\|[0054] In some cases, the reactor may comprise a first chamber for biomass generation (e.g., continuous, semi-continuous, membrane bioreactor), a second chamber for olivine dissolution (e.g., to optimize particle size and flow/recycle biomass), and a third chamber for biomass/suspended olivine separation (and for biomass return to the first chamber). In some cases, sea water based growth media may flow into and/or out of the first chamber. In some cases, CO2 from biomass growth may be provided to the second chamber. The second chamber may also receive biomass with siderophores from the first chamber. The second chamber may provide, in some cases, a recirculation loop for the biomass. The second chamber may be configured to provide the biomass without the siderophores to the third chamber. In some cases, the third chamber may be configured to return biomass to the first chamber. In some cases, the third chamber may be configured to provide the olivine and/or the biomass to seawater.\|[0055] The present disclosure effectively provides methods and designs for sustained microbial growth and siderophore production for olivine dissolution over long time periods. Current methods are unable to accelerate olivine dissolution with microbes for reaction volumes exceeding a few hundred milliliters, unlike the systems and methods disclosed herein. The presently disclosed systems and methods have been developed with the specific engineering and regulatory requirements needed to build large-scale, flow-through reactors with seawater that will then be returned to the local environment. The present disclosure effectively provides systems and methods for optimizing (1) strain selection for olivine dissolution, (2) grain size, (3) culturing conditions with natural seawater, and (4) the materials for the growth chamber.\|Optimizing Olivine\|[0056] [3] In another aspect, the present disclosure provides systems and methods for optimizing olivine for use in the field. Such optimization may comprise, for example, determining the optimal grain size distribution of olivine sand for use in carbon capture (covers combinations of grain size, color, blends, includes modeling grain size for specific sites); and physically and/or chemically processing the olivine (e.g., using machinery) to prepare one or more batches of carbon negative sand suitable for beach nourishment.\|Preparing Olivine\|[0057] [4] In another aspect, the present disclosure provides systems and methods for preparing olivine grains for optimal dissolution. The olivine grains may be part of a source material comprising olivine sand or a mixture comprising olivine sand and local sand.\|[0058] In some cases, the method may comprise crushing raw olivine to yield an optimal grain size and aggregating raw or crushed olivine into pellets. Such processing of the olivine may enhance dissolution of olivine, thereby accelerating the carbon capture process. In some cases, the method may further comprise selecting, milling, and/or matching olivine sand to native sediment for the purpose of coastal protection, beach nourishment and carbon capture.\|[0059] In another aspect, the present disclosure provides carbon-negative sand and processes for producing the same. The carbon-negative sand may comprise specially selected, prepared, and blended mineral particles which [1] are suitable to mitigate coastal erosion along coasts [2] react with carbon dioxide (CO2) and/or dissolved carbonic acid [H2CO3] to produce bicarbonate [HCO3-], [CO32-] ions, and/or solid-phase carbonate minerals [Ca, Mg]CO3, thus [3] simultaneously mitigating the impacts of climate change, ocean acidification, and coastal erosion.\|[0060] In order to be suitable for use in coastal erosion, beach nourishment, and marsh restoration projects, [4] manufactured carbon-negative sand and blends thereof should closely match the texture, grain size distribution, and color of native sediment. Thus, the processes for preparing carbon negative sand may be tailored such that the carbon-negative sand and blends thereof produce and achieve these specific pre-determined properties.\|[0061] In order to mitigate the impacts of carbon dioxide (ie. be "carbon negative"), [5] carbon negative sand may be manufactured from a mafic or ultramafic inorganic mineral or rock (typically naturally occurring olivine, basalt, serpentinite, brucite, wollastonite, or industrial-produced mineralequivalents such as slag). These minerals [6] may react with water and carbon dioxide and/or carbonic acid to produce bicarbonate ion as a reaction product, thereby decreasing the acidity of the surrounding fluid and converting the harmful carbon dioxide or carbonic acid into environmentally beneficial bicarbonate or carbonate ion. An example describing the reaction of forsterite olivine (Mg2SiO4) is provided below, although other minerals and rocks described in this disclosure result in equivalent reactions converting carbonic acid to bicarbonate ion:\| CO2 + H2O → H2CO3\| Mg2SiO4 + 4 H2CO3 → 2 Mg2+ + 4 HCO3- + H4SiO4\|[0062] In order to simultaneously achieve the engineering requirements of sand and sediment for coastal engineering, while preserving the chemical reactivity with carbon dioxide described above, [7] it may be necessary to prepare specially prepare the reactive mineral components and then blend these reactive components in specifically determined ratios with inert native or allochthonous sand and sediment to achieve the desired chemical, engineering, and aesthetic properties. This process is described in greater detail below:\|[0063] The process for preparing the CO2 - reactive component of carbon negative sand begins with a feedstock of mafic or ultramafic rocks, minerals, or their industrially produced equivalents. A list of potential feedstocks is provided in Table 1.\|[0064] Table 1. Potential feedstock materials for the production of the CO2 - reactive component of carbon negative sand.\|Naturally Occurring Rocks: Peridotite, Dunite, Harzburgite, Lherzolite, Basalt, Gabbro, Komatiite, SerpentineNaturally Occurring Minerals: Olivine, Forsterite, Fayalite, Enstatite, Pyroxene, Serpentine, BruciteIndustrial Byproducts: Blast-furnace Slag, Steel-furnace Slag, Basic-oxygen-furnace Slag, Electric-arc-furnace Slag, Ladle Slag.\|[0065] The preparation of the CO2 - reactive components of carbon negative sand may proceed via two critical steps:\| (1) The feedstock may be crushed and/or milled to increase the reactive surface area of the feedstock and provide fresh reactive surfaces for the reaction with carbon dioxide. Because the reaction occurs only on the surfaces of the grains and within microcracks created by the crushing/milling process, it is essential to increase the available reaction surface area to the maximum extent possible in order to maximize the material reactivity.\| (2) The crushed and milled material may then be size sorted using sieves, gravity separation, air classifiers, to provide a final product with a mean grain size and overall grain size distribution which meets the engineering specifications of the coastal engineering project. In some cases, this process may be designed to exclude excessive fine-grained material and/or coarser particles, to produce an intermediate grain-size material which closely matches the size distribution of the native sediment in the geographic region receiving the carbon negative sand. As an alternative to preparing batches of CO2 - reactive components individually, it is also possible to presort the material into various predetermined size ranges and then select and/or blend from these preclassified separates to achieve an overall blend suitable for use in a specific project.\|In most cases or all cases, the CO2 - reactive component may be further modified via mixing non-reactive sediment in order to achieve a combination of texture, color, and density, and engineering properties suitable for use in coastal engineering products. To achieve this, a third step may be required:\| (3) The CO2-reactive mineral component may be blended with one or more chemicallyinert sand and sediment materials to achieve a predetermined ratio providing the specified properties. A list of common non-reactive feedstocks is provided in Table 2. Blends consisting of 1-50% reactive component may be most common, but other variations of this invention, higher or lower fractions of the reactive component may be used.\|Table 2. Potential feedstock materials for the non-reactive component of carbon-negative sand.Naturally Occurring Native Sediment at the Project Site: May include native sand, silt, clay, organic matter and gravelNaturally Occurring Rocks/Sediment: Silicate Beach Sand, Carbonate Beach Sand, Dredged Sediment, Crushed Sandstone, Crushed Limestone, Carbonate OoidsNaturally Occurring Minerals: Quartz, Feldspar, Aragonite, Calcite, Garnet, Magnetite, Hematite, Limonite, Ilmenite, Smectite, Chlorite, Biotite, Muscovite, Rutile, Zircon and Monazite\|[0066] The goal of blending the reactive- and non-reactive sediment components is to achieve a final bulk product meeting various regulatory, aesthetic and engineering requires including color, texture, grain size, density, cohesion, hardness, etc. To realize a blended mixture between the reactive and non-reactive components of the carbon-negative sand mixture, the individual components may either be brought together in advance, or in alternate embodiments, separately conveyed or placed onto the project site in such a manner to realize an appropriate mixture over the duration of the project (ie. mixing between components occurs via the physical motion of sediment driven by conveyors, heavy equipment, and/or waves and tides).\|[0067] Although enhanced silicate weathering may be implemented in some instances, none of the prior work has [8] recognized and provided methods for the manufacture of engineered carbon-negative materials with specific suitable colors, grainsize, density, and reactivity required to meet specific regulatory, aesthetic, and engineering requirement for coastal engineering. Moreover, [9] prior work has completely neglected the engineering of these specific attributes in order to create safe and successful materials for coastal engineering applications. [10] No existing material used in present coastal engineering applications provides additional public and ecological benefits due to CO2 capture, alkalinity generation, and the mitigation of ocean acidification. Likewise, [11] no prior approaches have realized the simultaneous benefits derived from manufacturing carbon-negative materials which are suitable for coastal engineering, thus providing a dual benefit of mitigating coastal erosion and sea level rise.\|Carbon Credits\|[0068] [5] In another aspect, the present disclosure provides systems and methods for measuring, recording and verifying (MRV) carbon removal as well as ecological effects of olivine sand in carbon removal over large coastal areas. Such measurements, recording, and verification of carbon removal may be performed using one or more remote sensors, protocols for the use of such sensors (benthic flux chambers), and algorithms to interpret the data obtained and derived from the sensor readings. The presently disclosed systems may be used to prove the dissolution of olivine and the subsequent capture of CO2 based on the dissolution of the olivine. In some cases, the systems and methods disclosed herein may be implemented to predict dissolution (e.g., by utilizing one or more models for simulating or predicting olivine dissolution at a target site).\|[0069] The present disclosure also provides software configured to calculate CO2 consumption and to measure/record/verify carbon removal. The software may be configured to determine CO2 consumption and/or carbon removal based on one or more sensor readings and/or one or more input parameters. The one or more input parameters may relate to, for example, the physical or chemical properties of the olivine used, the ratio of olivine to sand, the location in which the olivine is distributed, an amount of olivine distributed to a target site, or the manner/configuration in which the olivine is distributed (e.g., method of distribution, form of distribution, or spatial characteristics of the distribution). In some cases, the sensor readings may comprise measurements of alkalinity, pCO2, pH, and/or water temperature.\|[0070] In one aspect, the present disclosure provides methods and protocols for measuring, recording, and verifying (MRV) carbon removal (e.g., by way of coastal carbon capture using olivine). Referring to FIG. 12, the protocols may be submitted to independent, third-party entities (e.g., academics, institutions, etc.) for validation. Once validated, the protocols may be implemented by an individual or an entity. Additional third-party entities may ensure and confirm compliance. The individuals or entities implementing the MRV protocols may then submit the third-party verified, compliant methodologies to a carbon credit verifier, and an offset or a credit may be issued on a registry for sale in domestic and/or international markets.\|[0071] FIGs. 13 - 14 and FIG. 37 show a reaction representing the chemical mechanism by which coastal carbon capture can occur when olivine is introduced to a target site (e.g., by adding olivine sand to beaches and mixing the olivine sand with the native beach sand). For every 1 mol of olivine (which olivine may comprise or exhibit any of the physical or chemical properties or compositions described herein), 4 mols of carbon dioxide may be consumed or captured, and 4 mols of an alkaline material (bicarbonate or HCO3-) may be generated.\|[0072] FIGs. 15 - 20 show an environment comprising a first layer comprising seawater and a second layer comprising sediment and pore water. The sediment and pore water may span a dimension of about 10 centimeters (cm) or about 4 inches (in). The reactions shown in and described in relation to FIGs. 13 - 14 and FIG. 37 may drive the capture of carbon dioxide (e.g., CO2 in the atmosphere or in the seawater) and the release of magnesium, bicarbonate, and silicic acid. The rate of the overall reaction may be determined based on the fluxes associated with CO2 capture and the subsequent release of magnesium, bicarbonate, and silicic acid.\|[0073] In some non-limiting embodiments, one or more stirrers may be used to facilitate the carbon capture process (e.g., by physically mixing the seawater containing olivine sediments with the medium comprising the carbon dioxide). The medium may comprise a liquid medium (e.g., seawater) or a gaseous medium (e.g., air comprising atmospheric carbon dioxide). In some non-limiting embodiments, one or more valves may be used to control and regulate an outflow of any products of the reaction (e.g., the magnesium, bicarbonate, and/or silicic acid).\|[0074] FIG. 21A illustrates a plot of a change in concentration of an alkaline material in a flux chamber as a function of time when the olivine-based carbon capture reactions of the present disclosure are used. The alkalinity of the medium in which the alkaline material is present may gradually increase over time. In some cases, the alkalinity may increase by a factor of 1.1 to 10 or more over a period of 1 to 10 days. As shown in FIG. 21B, the alkalinity flux with olivine increases more rapidly over time than the alkalinity flux at a control site in which olivine is not introduced. The alkalinity flux may correspond to the slope of the lines shown in these plots, and may have units of change in concentration of the alkaline material per unit time.\|[0075] FIG. 22 shows an overview of the porewater method for determining flux of an alkaline material that is produced. The porewater method may be based on Fick's first law of diffusion. The flux of the alkaline material may be determined based on a diffusion coefficient (representing area per unit time) and a dC/dZ value (representing a change in concentration or amount of substance per unit volume, as a function of position or dimensional length). With olivine present in porewater, a larger flux may be observed (steeper slope and bigger flux), whereas when olivine is not present, a smaller flux is observed (shallower slope and smaller flux).\|[0076] FIG. 23 shows a shrinking core model comprising a transformed volume and an untransformed volume of an exemplary olivine particle. The shrinking core model may be represented by X = 1 - [1 - R/(ρ∗d))∗t]^3, where X is the fraction of olivine reacted, R is a function of pH and temperature, p is molar density, d is starting diameter, and t represents time. One assumption for this model is that the particles are a perfect sphere.\|[0077] FIG. 24 shows dissolution rates for olivine having various grain sizes. The fraction of olivine reacted over time may increase more rapidly for olivine particles having smaller grain sizes. For example, for olivine with a 30 micrometer grain size, 10% of the olivine may react within 3 years, 50% of the olivine may react within 18 years, and 90% of the olivine may react within 47 years. In contrast, for olivine with a 64 micrometer grain size, 10% of the olivine may react within 6 years, 50% of the olivine may react within 39 years, and 90% of the olivine may react within 101 years. The rates shown generally correspond to static dissolution rates based on inorganic chemical processes, and may not include acceleration of weathering due to wave energy and biotic processes. The systems and methods of the present disclosure may be implemented to optimize dissolution rates by (1) inducing or imparting wave energy with a specific characteristic (e.g., periodicity, intensity, motion path, etc.) and/or (2) modifying the biotic processes used to enhance olivine dissolution.\|[0078] FIG. 25 shows an exemplary modeling approach for particle distribution. In one step, the modeling approach may comprise simulating grains to match a desired particle size distribution. The modeling approach may further comprise shrinking each particle over a time period (e.g., to simulate dissolution or erosion of one or more portions or layers of each particle), and thereafter summing the total mass of the particles and/or the total amount dissolved or eroded at various time points in order to determine the fraction of mass remaining as a function of time.\|[0079] FIG. 26 shows dissolution rates for different mixtures of olivine having different mean grain sizes. In general, olivine mixtures with smaller mean grain sizes may have a shorter half-life (i.e., a shorter time period for half of the olivine mixture to dissolve under a particular set of conditions).\|[0080] FIG. 27 shows the impact of temperature and pH on half-life. In some cases, the half-life for olivine dissolution may decrease as temperature increases. In some cases, the half-life for olivine dissolution may increase as pH increases. In some embodiments, the systems and methods disclosed herein may be implemented to optimize temperatures and pHs for dissolution environments to shorten the half-life for olivine dissolution. In other embodiments, the systems and methods disclosed herein may be implemented to identify candidate locations with optimal temperatures and pHs for olivine dissolution environments to shorten the half-life for olivine dissolution.\|[0081] The systems and methods disclosed herein may be configured or implemented to overcome challenges relating to spatial and temporal heterogeneity, low signal/noise ratios due to slow dissolution of olivine, and variation in secondary mineral product generation. The systems and methods disclosed herein may also help to overcome verification challenges such as, for example, objective criteria for acceptance and verification of carbon credit sales, and how to influence such criteria to adapt them to coastal weathering processes.\|[0082] The present disclosure provides methods for performing MRV (i.e., the measurement, recording, and verification) of carbon capture and/or olivine dissolution. In some cases, the methods may comprise establishing a treatment site and a reference or baseline site. The methods may further comprise measuring alkalinity fluxes and/or other parameters at a network of discrete locations. In some cases, this may be repeated over time as olivine dissolves over a series of time points. The methods may further comprise interpolating in time and space to determine an overall dissolution rate across an area or a volume of the site. In some cases, the overall dissolution rate across the site may be determined in part using a numerical reaction transport model that provides a fit to the measured data.\|[0083] FIG. 28 shows examples of temporal factors and spatial factors that can vary for coastal ecosystems, many of which are extremely dynamic. Temporal factors may include, for example, diurnal factors (i.e., day/night variations), tides, seasonality, temperature, weather, and/or waves. Spatial factors may include, for example, position and hydrodynamics, depth, tides, sediment type, grain size, sediment organic carbon content, and/or bottom cover (e.g., sea grass, rocks, coral, etc.).\|[0084] In some cases, the methods disclosed herein may comprise assessing or evaluating temporal heterogeneity by measuring depth, temperature, salinity, pH, turbidity, chlorophyll concentrations, and/or dissolved oxygen concentrations over time. FIG. 29 shows plots of temporal heterogeneity of various characteristics for a target site, including depth, salinity, turbidity, temperature, dissolved, oxygen, and pH. In some cases, the target site for olivine distribution and dissolution may be chosen based on temporal heterogeneity relative to other candidate or baseline/reference sites.\|[0085] As shown in FIGs. 30 - 32, in some cases, the methods disclosed herein may comprise calculating alkalinity fluxes and measuring dissolution rates of olivine to secure carbon credits. Alkalinity fluxes induced by olivine may be determined by discerning changes in alkalinity fluxes due to olivine from other natural background fluxes. In some cases, other fluxes attributable to olivine, such as dissolved inorganic carbon (DIC) fluxes and fluxes of pCO2, may be determined based on a comparison of measured fluxes to natural background fluxes. The fluxes attributable to olivine dissolution and/or the natural background fluxes may be space and time dependent. Such variations over space and time may be simulated, modeled, tracked, and/or measured to ensure accurate calculation of fluxes attributable to olivine, as opposed to natural background fluxes.\|[0086] In another aspect, the present disclosure provides various methods for accounting for heterogeneity for MRV. FIG. 33 shows a summary of the MRV approaches described below at different scales of cost and complexity.\|[0087] Approach 1 - In some cases, the methods may involve using the shrinking core model described elsewhere herein for an approximate rate of dissolution. The dissolution rate and CO2/olivine ratio may be assumed or approximated.\|[0088] Approach 2 - Alternatively, mesocosm experiments may be utilized to determine regional olivine dissolution rates. In cases where olivine is deployed in a target site (e.g., a mesocosm or the natural environment), olivine tracers may be used to track olivine dissolution in order to model and refine in situ weathering rates. The present disclosure provides systems and methods to track the movement of olivine grains in a target site. The systems and methods of the present disclosure may be implemented to track olivine transport in a target site based on or using, for example, trace metal content, fluorescent dyes, and/or olivine-specific spectral properties. This may be a relatively inexpensive process that can be set up prior to obtaining regulatory permits. Further, this approach may be initially tested using a sealed, recirculating design that is configured to maintain and control spatiotemporal heterogeneity and further allow for temperature and/or lighting control.\|[0089] Approach 3 - In some cases, the mesocosm-based approaches described herein may be augmented with field data (e.g., in situ data obtained manually or automatically using one or more sensors). The data obtained using the one or more sensors (which one or more sensors may comprise any of the sensors described herein or any other sensors for obtaining any of the measurements referred to herein) may provide additional information to better quantify and track spatial and/or temporal variations in environmental conditions or parameters relating to olivine dissolution and coastal carbon capture.\|[0090] Approach 4 - In some cases, a numerical model may be constructed that allows for accurate simulation of spatial and temporal variations in background fluxes and olivine dissolution rates. This can help to correct for time and space dependent variations, and allow for the use of sparse observations or other information or data at discrete points (e.g., points in time and/or points in space) to calibrate, verify, and validate the model. The model may be built and implemented for one or more a priori simulations.\|[0091] In cases where olivine is deployed in the natural environment, olivine tracers may be used to track olivine dissolution in order to estimate, predict, model, and refine in situ weathering rates. The present disclosure provides systems and methods for tracking the movement or transport of olivine grains in the natural environment (e.g., in a target site in which the olivine is provided or introduced). The systems and methods of the present disclosure may be implemented to track olivine transport based on or using, for example, trace metal content, fluorescent dyes, and/or olivine-specific spectral properties. The trace metal content, the movement or dispersion of fluorescent dyes, and/or the olivine-specific spectral properties may be detected and tracked using any of the sensors described herein.\|[0092] FIG. 34 illustrates various examples of reaction-transport modeling studies that may be used to simulate sediment porewater profiles, solid-phase chemistry, and benthic fluxes. The simulations and studies may be tailored to project requirements, and can take into account secondary clay mineralogy and Cr and Ni speciation and cycling. The plots shown in FIG. 34 illustrate an exemplary numerical simulation of alkalinity profile and the effects of spreading a 2 centimeter (cm) thick layer of pure olivine sand on a beach sediment. In some cases, the alkalinity flux across the sediment-water interface may be monitored by (1) constructing biogeochemical models of olivine dissolution in sediments, (2) validating model performance using field measurements of sediment-water alkalinity flux (and other carbonate parameters), and (3) calculating CO2 capture, storage, or sequestration (by weight or volume) based on the thermodynamics of air-sea CO2 exchange.\|[0093] The systems and methods disclosed herein may be implemented using one or more sensors capable of measuring at optimal spatial and temporal resolutions. The sensors may obviate the need to use traditional, manual geochemical methods, which require labor intensive field sampling and returning of samples to labs for analysis and can involve significant costs. FIG. 35 shows various examples of sensors that can be used for MRV, including sensors configured to measure temperature, salinity, pH, pCO2, DIC, alkalinity, and/or wave impacts on sand. In some cases, a solid state sensor for simultaneous measurement of total alkalinity and pH of seawater (including seawater that does or does not comprise olivine) may be used. In some embodiments, a plurality of sensors for MRV may be deployed on a single system. In other embodiments, a plurality of sensors for MRV may be deployed on multiple separate systems. Additional examples of sensors are shown in FIG. 36, including silicate sensors, alkalinity sensors, CTDO sensors, Cytochips, dissolved inorganic carbon sensors, and nitrate sensors. In some cases, a 29Si isotopic tracer can be used to track olivine dissolution and simultaneous precipitation of secondary clays and carbonate phases. This can allow separation of total and net silicate dissolution.\|[0094] In some cases, the impacts of physical wave-driven weathering on beach sand and olivine dissolution may be measured or simulated. In some cases, this may involve measuring and analyzing 2-phase (i.e., sand-water) flow in the benthic boundary layer of a breaking wave. This may be modeled numerically or physically (e.g., using wave tanks). In some cases, specialized sensors for measuring turbulent energy dissipation (e.g., in a lab or directly on a beach) may be utilized to measure impacts of physical wave-driven weathering.\|[0095] FIG. 38 illustrates an approach to measuring CO2 removal that is enabled by way of the reactions shown in FIG. 37. In some cases, it may not be feasible to monitor the air to sea CO2 flux. Measuring air-sea CO2 fluxes can be challenging because the olivine dissolution signal is strongly muted by dilution with open ocean seawater. For instance, a 1 cm thick layer of olivine dissolving in 5 meters of water in a bay with a 4-hour residence time implies a ~ 1.3 µM increase in water column alkalinity. Measuring net CO2 flux can also be complicated by extreme seasonal and diurnal variations in ΔPCO2air-sea due to changes in local photosynthesis and respiration. Accordingly, in some embodiments, the systems and methods disclosed herein may be implemented to monitor alkalinity flux across the sediment-water interface.\|[0096] In some cases, the models described herein (which models may be generated for specific sites) may undergo validation. Such validation may involve determining olivine abundance, spatial distribution, and dissolution rates at one or more reference points in space or time. In some cases, the reference points may be arranged in a grid pattern. Validation may further involve crossvalidating measured and modeled alkalinity fluxes and olivine dissolution at reference points, and calculating alkalinity flux for a region or a project based on (i) a known mass or volume of olivine deployed and (ii) validated site-specific modeling. The models may be validated using one or more sensor measurements as described elsewhere herein. Once validated, the models may be used to determine or predict olivine dissolution, reaction fluxes, and/or carbon sequestration. In some cases, the models may be updated or refined based on additional sensor measurements captured over a period of time. In some cases, the models may be revalidated based on additional sensor measurements.\|[0097] FIG. 39 illustrates an approach to calculating CO2 sequestration from alkalinity flux based on an expression of how water DIC storage changes as a function of increasing alkalinity. Seawater carbonate chemistry may be controlled by pCO2, pH, DIC, and alkalinity. An isocapnic quotient may be computed based on a change in alkalinity relative to a change in DIC, at fixed conditions for pCO2, temperature, and salinity. In some cases, a 1 micromol increase in alkalinity may yield a 0.78-0.93 micromol DIC increase, which means that for every one ton of forsterite provided to a target site, 0.97 to 1.16 tons of CO2 can be stored as marine DIC.\|[0098] FIG. 40 illustrates a plot showing seawater age and the depth below sea water level of the Atlantic Ocean as a function of latitude (degrees North). CO2 capture via ocean alkalinization requires that the enhanced alkalinity water mass achieves equilibrium with atmospheric pCO2. The precise timescale for pCO2 equilibrium (~ 4 months) and DIC adjustment (~4 years) depends on the Revelle factor (Jones et al. 2014). The time scale for air-sea equilibration is considerably shorter than the time scale for olivine dissolution (~ 10 - 100 year) and approximately similar to the transit time distribution of mixed layer and subtropical mode water (- 10 - 40 years). This means that the surface DIC reservoir can achieve quasi-steady equilibrium throughout equatorial and subtropical regions most suitable for coastal enhanced weather.\|[0099] FIG. 41 illustrates an exemplary CEW life cycle analysis. The life cycle may comprise mining and/or extracting olivine, grinding the olivine to approximately 400 micrometer grain sizes (or less), transporting the olivine to one or more target sites, and spreading the olivine at the target sites. In some cases, the life cycle may be at least about 89% efficient, and can enable sequestration of at least about 5 to 20 times more CO2 than the amount of CO2 emitted during mining, grinding, transportation, and/or spreading of olivine.\|[0100] FIG. 42 illustrates an example of a carbon payback period that can be realized using the methods and systems disclosed herein. In some cases, the break even payback period may occur at approximately 4 years, assuming the following:\| Grainsize: LE45 (d50: 365 µm)\| Temp: 25 °C\| pH: 8\| Embedded emissions: 110 tons CO2 / 1000 tons olivine\| Absorption efficiency: 3 moles ALK / mole olivine\| Dissolution constant: Log(r) = - 8.75 (can vary depending on pH/temp)\|[0101] FIG. 43 illustrates various plots showing exemplary olivine dissolution kinetics for olivine particles having different grain sizes. Dissolution time may decrease as olivine particle sizes decrease. The particle dissolution characteristics may be predicted or simulated using a shrinking core model and one or more laws, equations, or principles governing olivine dissolution rates. In some cases, the shrinking core model may be modified to permit the simulation of dissolution for realistic, commercially-available grain size distributions. The models described herein may be generated by modifying initial diagenesis models to incorporate olivine dissolution kinetics that correspond to the shrinking core model. The models may include and/or account for full carbonate chemistry (e.g., DIC, ALK, pCO2, pH, carbonate precipitation/dissolution) as well as biogeochemical processes (including aerobic and anaerobic respiration, formation of Fe/Mn oxides, pyrite, sulfide oxidation, etc).\|[0102] In some instances, secondary carbonate precipitation as shown in FIG. 44 can impact CO2 capture efficiency. Secondary carbonate precipitation may change the reactions described herein such that for every 1 mol of olivine introduced to a target environment, 2 moles of CO2 are consumed and 0 moles of alkalinity are generated. This can result in a 50% reduction in CO2 capture efficiency. The systems and methods disclosed herein may be implemented to minimize or reduce secondary carbonate precipitation. The rate of carbonate precipitation can be strongly controlled by local variations in geochemistry and biogenic calcification. In some cases, alkalinity export can be the dominant process occurring in sediments, and once mixed into the water column, consumption of alkalinity can be low given the long residence time of DIC and ALK in seawater.\|[0103] In some instances, secondary clay formation as shown in FIG. 45 can impact CO2 capture efficiency. Secondary clay formation may change the reactions described herein such that for every 1 mol of olivine, 8/3 moles of CO2 are consumed and 8/3 moles of alkalinity are generated. This can result in a 33% reduction in CO2 capture efficiency. The systems and methods disclosed herein may be implemented to minimize or reduce such secondary clay formation.\|[0104] In a related aspect, the present disclosure provides systems and methods for simulating a target site or environment. This can allow the study of olivine dissolution rates in a controlled environment, intermediate between lab and field conditions. Such systems and methods may be implemented to determine and/or monitor olivine dissolution rates, porewater geochemistry, or benthic flux measurements, study impacts of temperature on olivine dissolution and respiration, track impacts on seawater pH and other water chemistry, monitor ecological responses and air-sea water gas CO2 fluxes, track the fate, transport, and bioaccumulation of Cr and Ni, track the formation of secondary weathering products (e.g., Chrysotile, Carbonates, Clays), and monitor the impacts of olivine-based CO2 sequestration processes on benthic invertebrates/meiofauna.\|[0105] In some embodiments, the MRV methods and protocols disclosed herein may be adapted or adjusted for different types of olivine or for different target sites for olivine distribution. In such cases, the models used to predict or determine olivine dissolution, reaction fluxes, and/or carbon sequestration may be adjusted based on characteristics of the particular olivine/sand mixture used, the target site, and/or one or more sensor readings or measurements obtained in situ.\|Carbon Removal Prediction\|[0106] [6] In another aspect, the present disclosure provides systems and methods for predicting rates of carbon removal at specific sites. Such predictions may be based on, for example, data corresponding to measurement of changes in alkalinity, pCO2, pH, and/or water temperature. The predictions may be generated using algorithms and software interpreting such data. The algorithms and software may be implemented by way of one or more models that can be generated based on the MRV data obtained using various sensors as described elsewhere herein.\|[0107] In some embodiments, the predicted rates of carbon removal may be used to further optimize the carbon capture process. For instance, the predicted rates may be used to optimize the properties of the olivine sand, the preparation of the olivine sand, and/or the operation or the configuration of the reactor.\|Shipping and Deployment of Olivine\|[0108] [7] In another aspect, the present disclosure provides systems and methods for shipping and deploying olivine. In some cases, the shipping and deployment of olivine may be performed using a device for distributing carbon negative sand in shallow marine environments. The device may be, for example, a spreading device for spreading the olivine in a desired or optimal manner at a target site (e.g., a beach of interest).\|[0109] In some cases, the methods of the present disclosure may comprise determining whether one or more dredging modifications are needed in order to optimally distribute the carbon negative sand. Such determination may be based on one or more sensor readings and/or information about the target site in which the carbon negative sand is to be distributed.\|[0110] In some cases, the olivine may be processed before shipping to facilitate shipping and distribution of the olivine. For instance, the olivine may be modified to enable transportation of ultra-fine material (e.g., for reduction of liquefaction or capsizing risk.\|[0111] In some embodiments, various types and forms of maritime emissions reduction technology (e.g., an on-board olivine reactor driven by ship engine using ballast water) may be implemented. In some cases, bulk carrier direct deployment technology and related modifications (e.g., open sea distribution for in situ CEW) may be utilized. In some cases, grain washing and liquid alkalinity systems may be used for pre-deployment reduction of turbidity. In some cases, global logistics software may be used to mobilize idle maritime assets for carbon removal projects.\|[0112] FIG. 9 schematically illustrates an example of a system that may be used to deploy olivine for coastal nourishment. The system may comprise, for example, a split hulled hopper barge. In some cases, olivine may be mined and milled into carbon negative sand. Thereafter, the olivine may be loaded and shipped on dry bulk carriers to designated ports. The olivine may then be loaded into one or more split hulled hopper barges. In some embodiments, the barges may be linked together and towed to designated deployment sites. Once the barges are positioned at or near the designated deployment sites, the bottom of the barges may be configured to open in order to deploy the olivine. In some cases, sediment transport modeling may be used to predict where the olivine will move and/or in what directions the olivine will disperse.\|[0113] In a further aspect, the present disclosure provides a method and process for conducting carbon neutral and carbon negative dredging operations. The method and process of conducting dredging operations may be either net neutral or net negative with respect to atmospheric greenhouse gas emissions. To achieve this, dredged sediment may be mixed with one or more types of carbon negative sand, as described elsewhere herein. The methods and processes described herein may be adapted for any type of construction activity, including land-based construction activities.\|[0114] The dissolution of carbon negative sand may effect the conversion of gaseous and dissolved carbon dioxide into dissolved bicarbonate and carbonate ions, thereby increasing the capacity of fresh and salt water to store additional carbon in a dissolved state. When present as dissolved bicarbonate and carbonate ions, rather than carbon dioxide, these compounds may no longer contribute to climate change and can act to counter the effect of ocean acidification.\|[0115] In order to reduce, neutralize, or negate carbon dioxide emissions which occur during the combustion of fossil fuels during conventional dredging operations, a predefined ratio of carbon negative sand may be mixed with the dredging spoils in order to [1] result in the net capture of a specified amount of carbon dioxide and [2] ensure that the dredged sediments meet engineering and regulatory requirements for disposal or beneficial reuse. Blends consisting of 1-50% reactive carbon negative component may be most common, but in other variations, higher or lower fractions of the carbon negative component may be used.\|[0116] In order to mix carbon negative sand with dredged materials, several different approaches may be used depending on the type of dredging operation and intended fate of the dredged material. During cutterhead dredging operations, pump-out hopper dredging, and other approaches where dredged material is conveyed via a hydrologic slurry, the carbon negative sand may be directly mixed with the dredge spoils by injecting the carbon negative sand into the slurry pipeline. When using trailing suction hopper dredges, carbon negative sand may be mixed within a sediment hopper or barge prior to discharge. As an alternative, carbon negative sand may be directly placed at the sediment destination in the specified quantity and allowed to mix with the dredge spoils via the action of wind, waves, tides, and currents.\|[0117] Whereas traditional dredging operations consume large quantities of fuel fuels and emit correspondingly large quantities of greenhouse gasses, the method and process described here may allow dredging operations to be conducted in a way that is carbon neutral or even carbon negative over the lifetime of the project. This method and process provides significant advantages, allowing dredging operators to (i) mitigate carbon dioxide emissions on behalf of themselves or their clients, (ii) avoid emissions caps and taxes, and (iii) operate in jurisdictions which impose voluntary or involuntary restrictions on greenhouse gas emissions.\|Carbon-removing marine landfill cap\|[0118] In another aspect, the present disclosure provides carbon-removing marine landfill caps, processes for making the same, and processes for quantifying carbon capture from carbon-removing marine landfill caps. Marine landfills may serve as long-term, seafloor placement areas for unwanted construction debris, dredging materials, and toxic pollutants. Currently, marine landfills are often "capped" with non-toxic clay or sand or other similar materials to prevent contamination of overlying seawater and allow marine life to thrive in previously environmentally damaged areas. By using carbon-removing sand wholly, or as a constituent of, marine landfill caps, these sites can serve as climate change mitigation locales and further encourage the regeneration of environmentally damaged areas through the production of bicarbonate (alkalinity) which offsets ocean acidification and is beneficial for marine life.\|[0119] The process of making and deploying carbon-removing marine landfill cap differs from traditional marine landfill cap because 1) the depth (thickness) of carbon-removing cap sand 2) grain size distribution of carbon-removing cap sand, and 3) possible blend of carbon-removing cap and standard cap must be optimized to 1) prevent release of toxic pollutants and similar while allowing for sufficient permeability so that the carbon-removing sand will capture carbon over time and in particular not saturate sand porewaters such that the carbon removal reaction slows or stops. To achieve these objectives, a carbon-removing marine landfill cap may be deployed wholly as a cap, applied as a single mixture of carbon-removing cap to regular cap sand, or applied in layers where the percentage of carbon-removing cap sand to regular cap sand changes with depth, or the grain size distribution of carbon-removing cap and/or standard cap changes with depth. In all circumstances the carbon capture rates may vary with depth. In some cases, the carbon capture rate may be determined based on analytical measurements and sensor measurements from a particular site, fit to a global model. In some embodiments, the appropriate deployment technique described above may be a function of local wave climate, ecology (bioturbation), seawater temperature, landfill material, and an LCA (life cycle analysis) as the CO2 emitted to deploy the carbon-removing cap must be accounted for to insure the cap is, indeed, carbon-removing.\|Green Hydrogen\|[0120] [8] In another aspect, the present disclosure provides systems and methods for generating and using green hydrogen. As used herein, the term "green hydrogen" may refer to hydrogen that is produced from renewable energy sources and/or low-carbon power sources. The green hydrogen may be used as fuel for fuel cells or internal combustion engines. In some cases, the green hydrogen may be generated based on one or more products or reactants used to drive the CO2 capture and sequestration reactions/methods described elsewhere herein.\|Computer Systems\|[0121] In an aspect, the present disclosure provides computer systems that are programmed or otherwise configured to implement methods of the disclosure, e.g., any of the subject methods for processing and distributing olivine. FIG. 10 shows a computer system 1001 that is programmed or otherwise configured to implement a method for olivine processing and distribution. The computer system 1001 may be configured to, for example, (i) identify a target site, (ii) optimize one or more procedures for processing olivine to yield favorable properties or characteristics for the olivine, based on the target site identified, and (iii) coordinate transportation of the olivine to the target site. The computer system 1001 can be an electronic device of a user or a computer system that is remotely located with respect to the electronic device. The electronic device can be a mobile electronic device.\|[0122] The computer system 1001 may include a central processing unit (CPU, also "processor" and "computer processor" herein) 1005, which can be a single core or multi core processor, or a plurality of processors for parallel processing. The computer system 1001 also includes memory or memory location 1010 (e.g., random-access memory, read-only memory, flash memory), electronic storage unit 1015 (e.g., hard disk), communication interface 1020 (e.g., network adapter) for communicating with one or more other systems, and peripheral devices 1025, such as cache, other memory, data storage and/or electronic display adapters. The memory 1010, storage unit 1015, interface 1020 and peripheral devices 1025 are in communication with the CPU 1005 through a communication bus (solid lines), such as a motherboard. The storage unit 1015 can be a data storage unit (or data repository) for storing data. The computer system 1001 can be operatively coupled to a computer network ("network") 1030 with the aid of the communication interface 1020. The network 1030 can be the Internet, an internet and/or extranet, or an intranet and/or extranet that is in communication with the Internet. The network 1030 in some cases is a telecommunication and/or data network. The network 1030 can include one or more computer servers, which can enable distributed computing, such as cloud computing. The network 1030, in some cases with the aid of the computer system 1001, can implement a peer-to-peer network, which may enable devices coupled to the computer system 1001 to behave as a client or a server.\|[0123] The CPU 1005 can execute a sequence of machine-readable instructions, which can be embodied in a program or software. The instructions may be stored in a memory location, such as the memory 1010. The instructions can be directed to the CPU 1005, which can subsequently program or otherwise configure the CPU 1005 to implement methods of the present disclosure. Examples of operations performed by the CPU 1005 can include fetch, decode, execute, and writeback.\|[0124] The CPU 1005 can be part of a circuit, such as an integrated circuit. One or more other components of the system 1001 can be included in the circuit. In some cases, the circuit is an application specific integrated circuit (ASIC).\|[0125] The storage unit 1015 can store files, such as drivers, libraries and saved programs. The storage unit 1015 can store user data, e.g., user preferences and user programs. The computer system 1001 in some cases can include one or more additional data storage units that are located external to the computer system 1001 (e.g., on a remote server that is in communication with the computer system 1001 through an intranet or the Internet).\|[0126] The computer system 1001 can communicate with one or more remote computer systems through the network 1030. For instance, the computer system 1001 can communicate with a remote computer system of a user (e.g., an end user performing or monitoring the processing and/or the transportation or distribution of the olivine). Examples of remote computer systems include personal computers (e.g., portable PC), slate or tablet PC's (e.g., Apple® iPad, Samsung® Tab), telephones, Smart phones (e.g., Apple® iPhone, Android-enabled device, Blackberry®), or personal digital assistants. The user can access the computer system 1001 via the network 1030.\|[0127] Methods as described herein can be implemented by way of machine (e.g., computer processor) executable code stored on an electronic storage location of the computer system 1001, such as, for example, on the memory 1010 or electronic storage unit 1015. The machine executable or machine readable code can be provided in the form of software. During use, the code can be executed by the processor 1005. In some cases, the code can be retrieved from the storage unit 1015 and stored on the memory 1010 for ready access by the processor 1005. In some situations, the electronic storage unit 1015 can be precluded, and machine-executable instructions are stored on memory 1010.\|[0128] The code can be pre-compiled and configured for use with a machine having a processor adapted to execute the code, or can be compiled during runtime. The code can be supplied in a programming language that can be selected to enable the code to execute in a pre-compiled or ascompiled fashion.\|[0129] Aspects of the systems and methods provided herein, such as the computer system 1001, can be embodied in programming. Various aspects of the technology may be thought of as "products" or "articles of manufacture" typically in the form of machine (or processor) executable code and/or associated data that is carried on or embodied in a type of machine readable medium. Machine-executable code can be stored on an electronic storage unit, such as memory (e.g., read-only memory, random-access memory, flash memory) or a hard disk. "Storage" type media can include any or all of the tangible memory of the computers, processors or the like, or associated modules thereof, such as various semiconductor memories, tape drives, disk drives and the like, which may provide non-transitory storage at any time for the software programming. All or portions of the software may at times be communicated through the Internet or various other telecommunication networks. Such communications, for example, may enable loading of the software from one computer or processor into another, for example, from a management server or host computer into the computer platform of an application server. Thus, another type of media that may bear the software elements includes optical, electrical and electromagnetic waves, such as used across physical interfaces between local devices, through wired and optical landline networks and over various air-links. The physical elements that carry such waves, such as wired or wireless links, optical links or the like, also may be considered as media bearing the software. As used herein, unless restricted to non-transitory, tangible "storage" media, terms such as computer or machine "readable medium" refer to any medium that participates in providing instructions to a processor for execution.\|[0130] Hence, a machine readable medium, such as computer-executable code, may take many forms, including but not limited to, a tangible storage medium, a carrier wave medium or physical transmission medium. Non-volatile storage media including, for example, optical or magnetic disks, or any storage devices in any computer(s) or the like, may be used to implement the databases, etc. shown in the drawings. Volatile storage media include dynamic memory, such as main memory of such a computer platform. Tangible transmission media include coaxial cables; copper wire and fiber optics, including the wires that comprise a bus within a computer system. Carrier-wave transmission media may take the form of electric or electromagnetic signals, or acoustic or light waves such as those generated during radio frequency (RF) and infrared (IR) data communications. Common forms of computer-readable media therefore include for example: a floppy disk, a flexible disk, hard disk, magnetic tape, any other magnetic medium, a CD-ROM, DVD or DVD-ROM, any other optical medium, punch cards paper tape, any other physical storage medium with patterns of holes, a RAM, a ROM, a PROM and EPROM, a FLASH-EPROM, any other memory chip or cartridge, a carrier wave transporting data or instructions, cables or links transporting such a carrier wave, or any other medium from which a computer may read programming code and/or data. Many of these forms of computer readable media may be involved in carrying one or more sequences of one or more instructions to a processor for execution.\|[0131] The computer system 1001 can include or be in communication with an electronic display 1035 that comprises a user interface (UI) 1040 for providing, for example, a portal for a user to monitor the processing and/or the transportation or distribution of the olivine. The portal may be provided through an application programming interface (API). A user or entity can also interact with various elements in the portal via the UI. Examples of UI's include, without limitation, a graphical user interface (GUI) and web-based user interface.\|[0132] Methods and systems of the present disclosure can be implemented by way of one or more algorithms. An algorithm can be implemented by way of software upon execution by the central processing unit 1005. For example, the algorithm may be configured to identify a target site and optimize a procedure for processing the olivine based on the properties or the characteristics of the target site.\|[0133] While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. It is not intended that the invention be limited by the specific examples provided within the specification. While the invention has been described with reference to the aforementioned specification, the descriptions and illustrations of the embodiments herein are not meant to be construed in a limiting sense. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. Furthermore, it shall be understood that all aspects of the invention are not limited to the specific depictions, configurations or relative proportions set forth herein which depend upon a variety of conditions and variables. It should be understood that various alternatives to the embodiments of the invention described herein may be employed in practicing the invention. It is therefore contemplated that the invention shall also cover any such alternatives, modifications, variations or equivalents. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby.	(EP4166641)\|CROSS REFERENCE\|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/256,986 filed on October 18, 2021, U.S. Provisional Patent Application No. 63/281,575 filed on November 19, 2021, and U.S. Provisional Patent Application No. 63/298,412 filed on January 11, 2022, each of which is incorporated herein by reference in its entirety for all purposes.\|BACKGROUND\|[0002] Enhanced weathering or accelerated weathering may be used to remove atmospheric carbon dioxide by leveraging natural or artificially created minerals that can absorb and transform carbon dioxide into other substances through chemical reactions that may occur in the presence of water (e.g., in the form of rain, groundwater or seawater).\|SUMMARY\|[0003] The present invention relates to a system for processing olivine. More specifically, the present invention relates to a system for processing olivine wherein the system comprises a reactor for accelerating olivine weathering, more particularly, the reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering. Enhanced weathering may be used in marine environments to increase ocean alkalinity and atmospheric CO2 uptake. In some cases, enhanced weather may involve adding processed minerals directly to the ocean or dumping the processed minerals on beaches where wave action can disperse the processed minerals into the target marine environment. Enhanced weathering may be used to reduce CO2 levels in the atmosphere while also counteracting ocean acidification.\|[0004] Recognized herein are various limitations with current weathering methods, which may (i) involve long lead times and labor intensive procedures, (ii) impact ecological conditions (e.g., increasing water turbidity), and (iii) handling/processing of minerals that can pose additional ecological and health hazards via the possible ingestion, contact, or inhalation of fine grain of olivine mineral dust.\|[0005] The present application relates generally to using olivine to achieve enhanced weathering and increase CO2 uptake on accelerated timescales. In one aspect, the present disclosure provides systems and methods for accelerating weathering. In another aspect, the present disclosure provides a bioreactor configured to accelerate dissolution of olivine for weathering applications. In a further aspect, the present disclosure provides systems and methods for enhancing material properties of olivine. For example, the present disclosure provides a way to optimize the surface area effect of fine olivine grains by utilizing a binding process to bind or encapsulate the olivine fines into pellets of a larger effective grain size which can be more safely handled and distributed in the environment. The ability to tailor the design of pellets composed of olivine mineral fines by using different binding agents or encapsulation processes provides the ability to tailor and control the porosity, permeability, and degradation characteristics of the olivine-containing pellets, controlling their dissolution behavior in the environment. The systems and methods disclosed herein may enable efficient processing and deployment of olivine for purposes of CO2 capture in marine environments.\|[0006] In some embodiments, pelletized olivine aggregates formed from olivine fines may be prepared through a number of processes disclosed herein including [1] the use of a binding agent (such as but not limited to clay, polysaccharides, proteinaceous compounds, resin, plastic, glass, etc.) [2] via encapsulation of smaller olivine grains with said binding agent or other similar materials or [3] via the thermal fusion or physical compression of smaller olivine grains into larger aggregates.\|[0007] In some embodiments, the pellets may be designed to either [4] remain substantially intact while maintaining improved surface area via internal porosity and permeability or [5] degrade in a controlled fashion to release fine olivine fines to the environment in a prolonged controlled fashion. In some cases, [6] the preparation of such pellets may allow olivine dissolution to occur substantially faster than would occur for equivalently sized solid pure olivine grains, thereby improving the process of carbon capture while minimizing the aesthetic, health, and ecological harm and challenges posed by working with and utilizing olivine mineral fines.\|[0008] Another aspect of the present disclosure provides a non-transitory computer readable medium comprising machine executable code that, upon execution by one or more computer processors, implements any of the methods above or elsewhere herein.\|[0009] Another aspect of the present disclosure provides a system comprising one or more computer processors and computer memory coupled thereto. The computer memory comprises machine executable code that, upon execution by the one or more computer processors, implements any of the methods above or elsewhere herein.\|[0010] Additional aspects and advantages of the present disclosure will become readily apparent to those skilled in this art from the following detailed description, wherein only illustrative embodiments of the present disclosure are shown and described. As will be realized, the present disclosure is capable of other and different embodiments, and its several details are capable of modifications in various obvious respects, all without departing from the disclosure. Accordingly, the drawings and description are to be regarded as illustrative in nature, and not as restrictive.\|INCORPORATION BY REFERENCE\|[0011] All publications, patents, and patent applications mentioned in this specification are herein incorporated by reference to the same extent as if each individual publication, patent, or patent application was specifically and individually indicated to be incorporated by reference. To the extent publications and patents or patent applications incorporated by reference contradict the disclosure contained in the specification, the specification is intended to supersede and/or take precedence over any such contradictory material.\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0012] The novel features of the invention are set forth with particularity in the appended claims. A better understanding of the features and advantages of the present invention will be obtained by reference to the following detailed description that sets forth illustrative embodiments, in which the principles of the invention are utilized, and the accompanying drawings (also "Figure" and "FIG." herein), of which:\| FIG. 1 schematically illustrates the long-term carbonate-silicate cycle, in accordance with some embodiments.\| FIG. 2 schematically illustrates the chemical processes by which olivine can be used to capture and sequester CO2, in accordance with some embodiments.\| FIG. 3 schematically illustrates the chemical reactions that enable CO2 capture and sequestration using olivine, in accordance with some embodiments.\| FIG. 4 schematically illustrates olivine and mixtures of sand and olivine, in accordance with some embodiments.\| FIG. 5 schematically illustrates one exemplary method for using olivine to remove atmospheric CO2 and increase ocean alkalinity, in accordance with some embodiments.\| FIG. 6 schematically illustrates the use of wave energy to cause sand grains and/or olivine grains to collide and break into smaller pieces, thereby facilitating the dissolution of olivine, in accordance with some embodiments.\| FIG. 7 schematically illustrates an example of how the oceans can be used for natural carbon storage, in accordance with some embodiments.\| FIG. 8 schematically illustrates an example of a bioreactor, in accordance with some embodiments.\| FIG. 9 schematically illustrates an example of a system for deploying olivine for coastal nourishment, in accordance with some embodiments.\| FIG. 10 schematically illustrates a computer system that is programmed or otherwise configured to implement methods provided herein.\| FIG. 11 schematically illustrates an exemplary reactor configured to intake seawater that may be mixed with olivine and microbial biomass to generate alkalinity.\| FIG. 12 schematically illustrates an exemplary protocol for measuring, recording, and verifying (MRV) carbon removal, in accordance with some embodiments.\| FIGs. 13 - 14 schematically illustrate a chemical reaction by which coastal carbon capture occurs when olivine is introduced to a target site, in accordance with some embodiments.\| FIGs. 15 - 20 schematically illustrate an environment in which olivine can be introduced for costal carbon capture, in accordance with some embodiments.\| FIGs. 21A and 21B schematically illustrates a plot of concentration of an alkaline material in a flux chamber as a function of time, in accordance with some embodiments.\| FIG. 22 schematically illustrates an overview of the porewater method, in accordance with some embodiments.\| FIG. 23 schematically illustrates a shrinking core model, in accordance with some embodiments.\| FIG. 24 schematically illustrates dissolution rates for olivine having various grain sizes, in accordance with some embodiments.\| FIG. 25 schematically illustrates an exemplary modeling approach for particle distribution, in accordance with some embodiments.\| FIG. 26 schematically illustrates dissolution rates for different mixtures of olivine having different mean grain sizes, in accordance with some embodiments.\| FIG. 27 schematically illustrates the impact of temperature and pH on olivine half-life, in accordance with some embodiments.\| FIG. 28 schematically illustrates examples of temporal factors and spatial factors that can vary for coastal ecosystems, in accordance with some embodiments.\| FIG. 29 schematically illustrates plots of the temporal heterogeneity of various characteristics for a target site, in accordance with some embodiments.\| FIGs. 30 - 32 schematically illustrate examples of factors to consider when calculating alkalinity fluxes, in accordance with some embodiments.\| FIG. 33 shows a summary of various approaches for measuring, recording, and verifying carbon capture and olivine dissolution at different scales of cost and complexity, in accordance with some embodiments.\| FIG. 34 schematically illustrates various reaction-transport modeling studies that may be used to simulate sediment porewater profiles, solid-phase chemistry, and benthic fluxes, in accordance with some embodiments.\| FIGs. 35 - 36 schematically illustrate various examples of sensors that can be used for measuring, recording, and verifying carbon capture and/or olivine dissolution, in accordance with some embodiments.\| FIGs. 37 - 38 schematically illustrate reactions that may occur when olivine sand is introduced to beaches, in accordance with some embodiments.\| FIG. 39 schematically illustrates an approach to calculating CO2 sequestration from alkalinity flux based on an expression of how water DIC storage changes as a function of increasing alkalinity, in accordance with some embodiments.\| FIG. 40 schematically illustrates a plot showing seawater age and the depth below sea water level of the Atlantic Ocean as a function of latitude (degrees North), in accordance with some embodiments.\| FIG. 41 schematically illustrates an exemplary coastal enhanced weathering (CEW) life cycle analysis, in accordance with some embodiments.\| FIG. 42 schematically illustrates an example of a carbon payback period that can be realized using the methods and systems disclosed herein, in accordance with some embodiments.\| FIG. 43 schematically illustrates various plots showing exemplary olivine dissolution kinetics for olivine particles having different grain sizes, in accordance with some embodiments.\| FIG. 44 schematically illustrates the effects of secondary carbonate precipitation on CO2 capture efficiency, in accordance with some embodiments.\| FIG. 45 schematically illustrates the effects of secondary clay formation on CO2 capture efficiency, in accordance with some embodiments.\|DETAILED DESCRIPTION\|[0013] While various embodiments of the invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. Numerous variations, changes, and substitutions may occur to those skilled in the art without departing from the invention. It should be understood that various alternatives to the embodiments of the invention described herein may be employed.\|[0014] Whenever the term "at least," "greater than," or "greater than or equal to" precedes the first numerical value in a series of two or more numerical values, the term "at least," "greater than" or "greater than or equal to" applies to each of the numerical values in that series of numerical values. For example, greater than or equal to 1, 2, or 3 is equivalent to greater than or equal to 1, greater than or equal to 2, or greater than or equal to 3.\|[0015] Whenever the term "no more than," "less than," or "less than or equal to" precedes the first numerical value in a series of two or more numerical values, the term "no more than," "less than," or "less than or equal to" applies to each of the numerical values in that series of numerical values. For example, less than or equal to 3, 2, or 1 is equivalent to less than or equal to 3, less than or equal to 2, or less than or equal to 1.\|[0016] The term "real time" or "real-time," as used interchangeably herein, generally refers to an event (e.g., an operation, a process, a method, a technique, a computation, a calculation, an analysis, a visualization, an optimization, etc.) that is performed using recently obtained (e.g., collected or received) data. In some cases, a real time event may be performed almost immediately or within a short enough time span, such as within at least 0.0001 millisecond (ms), 0.0005 ms, 0.001 ms, 0.005 ms, 0.01 ms, 0.05 ms, 0.1 ms, 0.5 ms, 1 ms, 5 ms, 0.01 seconds, 0.05 seconds, 0.1 seconds, 0.5 seconds, 1 second, or more. In some cases, a real time event may be performed almost immediately or within a short enough time span, such as within at most 1 second, 0.5 seconds, 0.1 seconds, 0.05 seconds, 0.01 seconds, 5 ms, 1 ms, 0.5 ms, 0.1 ms, 0.05 ms, 0.01 ms, 0.005 ms, 0.001 ms, 0.0005 ms, 0.0001 ms, or less.\|Overview\|[0017] To avoid the worst effects of climate change, we must rapidly remove billions of tons of CO2 from the atmosphere. There are currently no proven methods for doing so. There is an urgent need to identify carbon removal methods that are permanent, scalable, and economical.\|[0018] The earth's natural long-term carbonate-silicate cycle is how our planet has naturally captured CO2 over thousands of years. Over millennia, rain falling on exposed volcanic rock causes it to weather, which removes CO2 from the atmosphere as bicarbonate dissolved in water. This water flows to the oceans, where marine calcifying organisms incorporate the CO2 into their shells and skeletons. When they die, they form ocean sediment, ultimately becoming limestone.\|[0019] The systems and methods of the present disclosure enable the acceleration of Earth's natural carbon removal method of rock weathering, through the extraction, processing (e.g., crushing and/or grinding), and transportation of volcanic mineral olivine to coastlines for dispersal or distribution. In some embodiments, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process. In other embodiments, a bioreactor may be used to enhance and facilitate olivine dissolution. In either case, carbon dioxide may be removed from the atmosphere as the olivine breaks down.\|[0020] Coastal Carbon Capture, also known as Coastal Enhanced Weathering, can be categorized as a negative emission technology (NET) that removes and stores CO2 on long timescales (tens to hundreds of thousands of years). The process aims to accelerate the natural chemical weathering of the mineral olivine by spreading large amounts of ground olivine-containing rock onto coastlines or bioreactors positioned on or near such coastlines, where it can dissolve in seawater, thereby increasing the rate of CO2 absorption by the ocean.\|[0021] The present disclosure provides systems and methods for accelerating the Earth's natural carbon removal method of rock weathering, by extracting the volcanic mineral olivine, grinding it into sand, and deploying it on coastlines or in bioreactors located on said coastlines. There, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process. Carbon dioxide is removed from the atmosphere as the olivine breaks down.\|[0022] FIG. 1 illustrates the long-term carbonate-silicate cycle. The illustrated reaction is the foundation of the Long-Term Inorganic Carbon Cycle, which has been occurring for billions of years, stabilizing Earth's atmospheric CO2 concentrations, and in turn enabling life to thrive. In fact, carbon dioxide removal (CDR) through natural rock weathering consumes ~1 gigaton of CO2 every year. Natural CO2 removal through rock weathering may be achieved through the following steps:\| 1. Rain falls on volcanic rocks, slowly dissolving them.\| 2. Carbonic acid dissolved in the rainwater reacts with silicate from the rocks, shifting the equilibrium from carbonic acid to bicarbonate.\| 3. This bicarbonate flows to the ocean.\| 4. Marine organisms use this as calcium carbonate in their shells and skeletons; when they die this becomes limestone.\| 5. Limestone formed at the ocean floor eventually subducts, locking up the carbon for millions of years.\|[0023] FIG. 2 illustrates the chemical processes that are enabled by olivine to perform CO2 capture and sequestration. FIG. 3 illustrates the chemical reactions that enable CO2 capture and sequestration using olivine. As the olivine dissolves, its products are magnesium ions (the second most abundant ion in the ocean behind sodium), silicate (used by diatoms to build their skeletons) and dissolved carbon. Referring to FIG. 2 and FIG. 3, when olivine dissolves in water, it drives the illustrated reaction, thus increasing CO2 uptake, raising pH, and generating alkalinity. As a result, this process has the potential co-benefit of counteracting ocean acidification. Ocean acidification is the process by which increasing atmospheric CO2 dissolves in seawater, which reduces pH (increasing acidity) (upper reaction in diagram below). This reduces the ability of calcifying organisms like corals to grow and produce exoskeletons, or shells. As shown in FIG. 2 and FIG. 3, dissolving olivine in water sequesters hydrogen ions into dissolved silicate (H4SiO4), a molecule that can be used by diatoms, an important photosynthesizing algae that fixes carbon dioxide and forms the base of food web.\|[0024] Unfortunately, natural chemical weathering happens too slowly to balance human CO2 emissions and is already accounted for in Earth's present-day carbon budget. The systems and methods disclosed herein can be deployed and implemented to accelerate this natural process to remove at least a gigaton of atmospheric CO2 per year on a global scale.\|Accelerating a Natural Process\|[0025] Coastal Carbon Capture can be used to accelerate Earth's natural CO2 removal process. At current rates, the natural process of rock weathering through rainfall needs to be sped up by at least 100 times to absorb the CO2 emitted by human activity. Coastal Carbon Capture (CCC) can accelerate the process by using wave energy and/or bioreactors to break down olivine. The rock containing the olivine may be placed in high-energy coastal environments, where wave energy mechanically activates the rock, causing collisions which remove the silica coating and efficiently grind the olivine down. The olivine sand then dissolves in the water at a rate orders of magnitude faster than in the geological process.\|[0026] Coastal Carbon Capture may comprise the following steps:\| 1. Extract olivine and efficiently grind it. Olivine is a green volcanic silicate mineral. It is highly abundant and found near the surface all over the world. Olivine rocks can be efficiently crushed to sand and gravel grain sizes.\| 2. Transport olivine to a nearby coastal area. The olivine sand may be transported (e.g., by rail, ship, or truck) to a nearby coastal shelf sea. There, it may be spread in a thin layer.\| 3. Wave energy may accelerate CO2 removal. Wave energy and currents may further grind down the olivine. Grain-on-grain collisions can cause fine fraction particles (< 10 microns) to form, which then weather very rapidly. The olivine may consequently dissolve in the water rapidly, accelerating the reaction which removes CO2 from the ocean/atmosphere.\|[0027] FIG. 5 illustrates one exemplary method for using olivine to remove atmospheric CO2 and increase ocean alkalinity. As shown in FIG. 6, wave energy may cause sand grains and/or olivine grains to collide and break into smaller pieces, thereby facilitating the dissolution of olivine.\|Olivine\|[0028] Olivine is a common, naturally occurring volcanic mineral, with physical properties similar to quartz. Olivine may be 23% denser than quartz sand (1.43 tons/cy). Olivine sand is a clean upland sand that is 25% denser than silicate sand, and that can be artificially milled to match native grain size. Darker and lighter olivine sources allow for color matching to the native sand color.\|[0029] Olivine can be processed to yield fine olivine grains with increased surface area exposure, which can speed up dissolution and the CO2 capture process. The olivine dissolution and CO2 capture process can also be accelerated by (i) using reactive and soluble minerals, (ii) increasing an amount of surface area of the olivine grains that is exposed to a solvent (e.g., water or seawater), (iii) enhancing fluid-mineral interactions, and/or (iv) reducing or eliminating secondary mineral coatings or the formation of secondary weathering products (e.g., precipitation of secondary clays and carbonate phases).\|[0030] Once deployed on a beach, olivine can capture 20 times more carbon than is emitted in the mining, milling, shipping, and beach nourishment operation. 1 ton of olivine sand can capture up to 1.25 tons of carbon in ideal situations. Since it takes olivine several decades to weather, it will provide effective coastal protection during long-term beach nourishment cycles.\|[0031] One type of olivine may be white olivine, or Forsterite (Mg2SiO4). This is a magnesium rich form of olivine, known as Forsterite (Mg2SiO4). Weathering 1 ton of olivine can remove up to 1.25 tons of CO2 from the atmosphere.\|[0032] FIG. 4 illustrates olivine and mixtures of sand and olivine. In some cases, the olivine may be mixed with natural beach sand before the olivine is deployed at a target site. The mixture comprising the olivine may comprise at least about 5%, 10%, 15%, 20%, 25%, or 30% olivine by weight or volume. In some cases, the mixture may comprise more than 30% olivine by weight or volume. In some cases, the mixture may comprise less than 5% olivine by weight or volume. In some cases, the mixture may comprise between about 5% and about 30% olivine by weight or volume.\|[0033] Beneficial applications of olivine include, for example, Marsh Restoration, Coastal Engineering/Hazard Mitigation, and CO2 Capture. As described above, olivine sand can react with water and CO2. CO2 may dissolve in water to form carbonic acid. Olivine dissolution may consume the carbonic acid to yield soluble bicarbonate ion (baking soda). This can: Lower atmospheric CO2, Neutralize ocean acidification, and Support the growth of calcifying organisms (Corals, etc).\|[0034] In some cases, olivine sand may be provided to municipalities to augment the sediment used in beach nourishment projects. As the sand weathers, it captures carbon. The sand and its placement are paid for by carbon credits. Therefore, the greater the percentage of olivine sand mixed into the native sand, the cheaper the beach nourishment project. A 10% mix would mean a -10% decrease in sand cost. Through the use of olivine sand, beach nourishment can play a critical role in reversing climate change and ocean acidification if the right mix of native and olivine sand is used. At scale, over a billion tons of CO2 could be removed from the atmosphere every year.\|[0035] Using wave action to break down the olivine is critical to the life cycle. Past analyses have shown that grinding the olivine down to <100µm size is highly energy-intensive. However, grinding the olivine down to >300µm gravel requires far less energy. Using the natural, free energy of water movement to break the olivine down further reduces the milling and grinding energy to a small proportion of the total.\|[0036] Co-Benefits of the methods described herein include, for example: reduction in Ocean Acidification (OA). Ocean acidification has been shown to damage marine ecosystems. Olivine increases local pH levels, potentially mitigating the adverse effects of OA on marine ecosystems. This could potentially improve aquaculture and fishery yields, bolstering local economies at deployment sites as well as reversing damage to marine ecosystems. FIG. 7 illustrates an example of how the oceans can be used for natural carbon storage. Excess CO2 emissions may increase ocean acidity. The systems and methods of the present disclosure may be implemented to reduce acidity and help the oceans safely store more CO2 as bicarbonate.\|[0037] Co-Benefits of the methods described herein may also include, for example: support for diatom growth. Diatoms, marine photosynthetic microalgae, are a cornerstone of marine food webs and capture CO2 through photosynthesis, creating 40% of oxygen on Earth. Diatom abundance has decreased as CO2 has risen, partly due to decreasing concentrations of silicate in the ocean due to damming of rivers limiting sediment flow. Since olivine is primarily magnesium silicate, the increase in silicate concentrations from olivine dissolution may lead to diatom growth. Increases in diatoms would increase the health of marine ecosystems and support photosynthetic carbon capture. Other co-benefits can include, for example, supporting coastal communities facing enhanced coastal erosion and sea level rise by supplying a low-cost source of sediment (which may be paid for using carbon credits).\|Mechanics of Weathering\|[0038] In some cases, grain-on-grain collisions may rapidly break down the olivine. Olivine grains may be reduced in size due to mechanical activation. In some cases, the motion of the water in which the olivine is provided may cause surface abrasions. In some cases, the surface of the olivine grains may be mechanically activated to enable and/or enhance CO2 uptake and de-acidification.\|Sensors\|[0039] In some cases, one or more sensors may be used to track, monitor, and quantify olivine dissolution, CO2 uptake, and ocean de-acidification. The measurements obtained using the sensors may be used to adjust the preparation or processing of the olivine, the optimal properties of the olivine, the location in which the olivine is introduced, the rate at which the olivine is introduced, a method by which the olivine is distributed, or a configuration/form in which the olivine is distributed.\|[0040] In some cases, the one or more sensors may be used to monitor and track: Olivine Dissolution Rates (Porewater Geochemistry, Benthic Flux Measurements), Impacts on Water Chemistry, Ecological Response, Fate, Transport and Bioaccumulation of Cr and Ni, and/or Formation of Secondary Weathering Products (Chrysotile, Carbonates, Clays). In some cases, an isotopic tracer along with [Si] and [ALK] measurements may be used to track olivine dissolution and simultaneous precipitation of secondary clays and carbonate phases. The sensors may also be used to track olivine grains over time [ie physical tracking of olivine using dyes / tracers, etc.].\|Reaction-Transport Modeling\|[0041] In some cases, simulation models may be used to optimize the preparation or processing of the olivine, the properties of the olivine, the location in which the olivine is introduced, the rate at which the olivine is introduced, a method by which the olivine is distributed, or a configuration/form in which the olivine is distributed. The models may be configured to simulate sediment porewater profiles, Water column and Porewater Chemistry (e.g., pCO2, DIC, pH, DO, TA, Nutrients, Metals, DOC), solid-phase chemistry and benthic fluxes, Secondary Clay Mineralogy, and Cr and Ni speciation and cycling. In some cases, the models may be used for simulation of the effects of spreading layers of olivine sand of varying thicknesses on a target beach sediment with one or more known biological, chemical, or ecological properties or characteristics.\|[0042] In some cases, the models may be used simulate or predict Olivine Dissolution Rates, study the impacts of Temperature of Olivine Dissolution & Respiration, track impacts on seawater pH, track Air-Sea Water Gas CO2 Fluxes, monitor and evaluate fate and transport of Cr and Ni, assess the impacts on benthic invertebrates/meiofauna, track sediment characteristics (e.g., changes in mineralogy, formation of secondary carbonate/clays), monitor the impacts of Meteorology and Hydrology (e.g., temperature, wind speed/direction, precipitation, salinity, turbidity, current), or simulate Physical Sediment Transport and/or Olivine Redistribution.\|Method of Removing Atmospheric Carbon\|[0043] [1] In one aspect, the present disclosure provides a method for removing atmospheric carbon using olivine dissolution technologies. The method may be implemented using natural wave energy (i.e., in situ coastal enhanced weathering (CEW)) and/or applied energy (i.e., closed-system artificial weathering of olivine in a man-made reactor or a sand pit resulting from coastal nourishment projects or dredging).\|Bioreactor\|[0044] In another aspect, the present disclosure provides systems and methods to accelerate olivine dissolution reactions in a bioreactor. The bioreactor may comprise one or more internal chambers for housing or storing olivine for any amount of time. The bioreactor may comprise one or more openings or inlets for receiving olivine. The olivine may comprise pure olivine or a mixture of olivine and sand or other elements or materials. The olivine may be unprocessed. Alternatively, the olivine may be processed or pre-processed (e.g., by grinding).\|[0045] In some cases, the bioreactor may comprise one or more mechanical components for mechanical weathering of the olivine. The mechanical weather may cause grain-on-grain collisions that may rapidly break down the olivine. Olivine grains may be reduced in size due to mechanical activation. In some cases, the bioreactor may be in fluid communication with water. In some cases, the bioreactor may comprise an internal chamber for housing the water and/or the olivine. The motion of the water in which the olivine is introduced may cause surface abrasions. In some cases, the surface of the olivine grains may be mechanically activated to enable and/or enhance CO2 uptake and ocean de-acidification.\|[0046] In some cases, the mechanical components may comprise one or more gears or actuators for inducing a motion that cause mechanical weathering of the olivine. The motion may be a linear motion, or a rotational motion, or any combination thereof.\|[0047] In some cases, the bioreactor may comprise a chamber for housing one or more microbial products or other biological mediators and/or enzymatic accelerants that can help to further break down the olivine. The chamber housing the microbial products may be in fluid communication with (i) the chamber housing the olivine, (ii) the chamber that is in fluid communication with the ocean water, or both (i) and (ii).\|[0048] FIG. 8 schematically illustrates an example of a bioreactor 800. The bioreactor 800 may be configured to receive olivine, which olivine may or may not be pre-processed (e.g., by grinding or crushing). The olivine may be stored within a first chamber 810 of the bioreactor 800 for further processing. In some cases, the bioreactor 800 may comprise a second chamber 820 configured to house one or more microbial products or other biological mediators and/or enzymatic accelerants that can help to further break down the olivine. In some cases, the bioreactor 800 may comprise a third chamber 830. The third chamber 830 may comprise a reaction chamber in fluid communication with the first chamber 810 and the second chamber 820. The third chamber 830 may be used to break down the olivine using the microbial products or other biological mediators and/or enzymatic accelerants. Once broken down, the processed olivine may be provided to a target region external to the bioreactor 800 to facilitate CO2 capture and sequestration.\|Microbes\|[0049] [2] In another aspect, the present disclosure provides a method for enhanced dissolution of olivine through (1) microbial products or other biological mediators and (2) enzymatic accelerants. The method may comprise enhancing dissolution of olivine in an olivine reactor or sand pit resulting from coastal nourishment projects or dredging through: microbial products or other biological mediators; and enzymatic accelerants.\|[0050] In another aspect, the present disclosure provides systems and methods for olivine dissolution by microorganisms, biological organisms, and/or biological mechanisms. The dissolution of olivine in water may consume protons and increase alkalinity, thereby removing dissolved aqueous CO2. This aqueous CO2 removal may induce additional CO2 to be taken up from the atmosphere and subsequently converted to bicarbonate, carbonate, and/or solid-phase carbonate minerals, thereby sequestering carbon for long time periods [1]. Scaling and accelerating this process has the potential to mitigate climate change and ocean acidification.\|[0051] In some cases, the reactors disclosed herein may be designed to grow particular microbial strains in an aqueous medium in order to induce metabolic states that can accelerate olivine dissolution. In circum-neutral pH naturally oxygenated waters, ferric iron (Fe2+) contained within olivine may be rapidly oxidized to ferrous iron (Fe3+) by oxygen even in the absence of microbial activity [2]. This oxidized iron can form a surface layer of Fe-oxyhydroxides on the mineral surface of olivine which can shield portions of its total surface area from contact with solution [3]. These Fe-oxyhydroxide surface coatings can, in some cases, impede olivine dissolution [4].\|[0052] For the vast majority of organisms, Fe is a required nutrient and a key component of many cellular proteins. However, most Fe in naturally oxygenated waters at circum-neutral pH is insoluble and typically complexed to particles. Certain microorganisms can produce organic compounds known as siderophores to mobilize and acquire insoluble iron on mineral surfaces [2], which can concurrently increase olivine mineral dissolution rates [3]. However, the production of siderophores may be regulated by Fe availability to the cells. As more Fe is acquired by the cells (i.e. the less iron-limited they are), siderophore production may decrease, which may slow dissolution rates. Hence, in order to sustain and scale siderophore production over extended time periods in large reactors, numerous interacting factors may be optimized:\| 1. The most optimized biological strains (these may be identified through a series of experiments, and in some cases, custom strains may be generated either through directed evolution or genetic editing).\| 2. The optimal ratios of microbial to siderophore concentrations given certain growth conditions.\| 3. Olivine dissolution optimization as a function of particle size/surface area and flow rate from biomass generation.\| 4. Optimized long-term growth conditions for sustained siderophore production.\| 5. Optimized reactor design series including appropriate materials to avoid silicate and trace metal contamination.\| 6. Development of mathematical model to optimize siderophore production yield, biomass generation, and olivine dissolution.\| 7. Development of appropriate parameters to track to feed into the model.\| 8. Development of any treatment of seawater effluent prior to returning to the ocean.\| 9. Development of a model that calculates CO2 sequestration from the addition of alkalinized seawater to the local ocean region.\|System Design\|[0053] Referring to FIG. 11, the illustrated reactor may be configured to intake seawater that may be mixed with olivine and microbial biomass to generate alkalinity. Depending on the source, seawater may have to be pretreated prior to reacting with olivine. This reaction may also result in trace metals, microbial biomass, and other reaction products mixing in with the seawater medium. In order to sequester carbon at scale, this alkaline seawater may be returned to the ocean to induce atmospheric CO2 uptake. Importantly, the return of this seawater containing the certain constituents must meet local regulations. Another microbially-mediated treatment process that returns effluent to the environment may involve anaerobic digestion. This may be a good reference to understand regulations for effluent from microbial processes.\|[0054] In some cases, the reactor may comprise a first chamber for biomass generation (e.g., continuous, semi-continuous, membrane bioreactor), a second chamber for olivine dissolution (e.g., to optimize particle size and flow/recycle biomass), and a third chamber for biomass/suspended olivine separation (and for biomass return to the first chamber). In some cases, sea water based growth media may flow into and/or out of the first chamber. In some cases, CO2 from biomass growth may be provided to the second chamber. The second chamber may also receive biomass with siderophores from the first chamber. The second chamber may provide, in some cases, a recirculation loop for the biomass. The second chamber may be configured to provide the biomass without the siderophores to the third chamber. In some cases, the third chamber may be configured to return biomass to the first chamber. In some cases, the third chamber may be configured to provide the olivine and/or the biomass to seawater.\|[0055] The present disclosure effectively provides methods and designs for sustained microbial growth and siderophore production for olivine dissolution over long time periods. Current methods are unable to accelerate olivine dissolution with microbes for reaction volumes exceeding a few hundred milliliters, unlike the systems and methods disclosed herein. The presently disclosed systems and methods have been developed with the specific engineering and regulatory requirements needed to build large-scale, flow-through reactors with seawater that will then be returned to the local environment. The present disclosure effectively provides systems and methods for optimizing (1) strain selection for olivine dissolution, (2) grain size, (3) culturing conditions with natural seawater, and (4) the materials for the growth chamber.\|Optimizing Olivine\|[0056] [3] In another aspect, the present disclosure provides systems and methods for optimizing olivine for use in the field. Such optimization may comprise, for example, determining the optimal grain size distribution of olivine sand for use in carbon capture (covers combinations of grain size, color, blends, includes modeling grain size for specific sites); and physically and/or chemically processing the olivine (e.g., using machinery) to prepare one or more batches of carbon negative sand suitable for beach nourishment.\|Preparing Olivine\|[0057] [4] In another aspect, the present disclosure provides systems and methods for preparing olivine grains for optimal dissolution. The olivine grains may be part of a source material comprising olivine sand or a mixture comprising olivine sand and local sand.\|[0058] In some cases, the method may comprise crushing raw olivine to yield an optimal grain size and aggregating raw or crushed olivine into pellets. Such processing of the olivine may enhance dissolution of olivine, thereby accelerating the carbon capture process. In some cases, the method may further comprise selecting, milling, and/or matching olivine sand to native sediment for the purpose of coastal protection, beach nourishment and carbon capture.\|[0059] In another aspect, the present disclosure provides carbon-negative sand and processes for producing the same. The carbon-negative sand may comprise specially selected, prepared, and blended mineral particles which [1] are suitable to mitigate coastal erosion along coasts [2] react with carbon dioxide (CO2) and/or dissolved carbonic acid [H2CO3] to produce bicarbonate [HCO3-], [CO32-] ions, and/or solid-phase carbonate minerals [Ca, Mg]CO3, thus [3] simultaneously mitigating the impacts of climate change, ocean acidification, and coastal erosion.\|[0060] In order to be suitable for use in coastal erosion, beach nourishment, and marsh restoration projects, [4] manufactured carbon-negative sand and blends thereof should closely match the texture, grain size distribution, and color of native sediment. Thus, the processes for preparing carbon negative sand may be tailored such that the carbon-negative sand and blends thereof produce and achieve these specific pre-determined properties.\|[0061] In order to mitigate the impacts of carbon dioxide (ie. be "carbon negative"), [5] carbon negative sand may be manufactured from a mafic or ultramafic inorganic mineral or rock (typically naturally occurring olivine, basalt, serpentinite, brucite, wollastonite, or industrial-produced mineralequivalents such as slag). These minerals [6] may react with water and carbon dioxide and/or carbonic acid to produce bicarbonate ion as a reaction product, thereby decreasing the acidity of the surrounding fluid and converting the harmful carbon dioxide or carbonic acid into environmentally beneficial bicarbonate or carbonate ion. An example describing the reaction of forsterite olivine (Mg2SiO4) is provided below, although other minerals and rocks described in this disclosure result in equivalent reactions converting carbonic acid to bicarbonate ion:\| CO2 + H2O → H2CO3\| Mg2SiO4 + 4 H2CO3 → 2 Mg2+ + 4 HCO3- + H4SiO4\|[0062] In order to simultaneously achieve the engineering requirements of sand and sediment for coastal engineering, while preserving the chemical reactivity with carbon dioxide described above, [7] it may be necessary to prepare specially prepare the reactive mineral components and then blend these reactive components in specifically determined ratios with inert native or allochthonous sand and sediment to achieve the desired chemical, engineering, and aesthetic properties. This process is described in greater detail below:\|[0063] The process for preparing the CO2 - reactive component of carbon negative sand begins with a feedstock of mafic or ultramafic rocks, minerals, or their industrially produced equivalents. A list of potential feedstocks is provided in Table 1.\|[0064] Table 1. Potential feedstock materials for the production of the CO2 - reactive component of carbon negative sand.\|Naturally Occurring Rocks: Peridotite, Dunite, Harzburgite, Lherzolite, Basalt, Gabbro, Komatiite, SerpentineNaturally Occurring Minerals: Olivine, Forsterite, Fayalite, Enstatite, Pyroxene, Serpentine, BruciteIndustrial Byproducts: Blast-furnace Slag, Steel-furnace Slag, Basic-oxygen-furnace Slag, Electric-arc-furnace Slag, Ladle Slag.\|[0065] The preparation of the CO2 - reactive components of carbon negative sand may proceed via two critical steps:\| (1) The feedstock may be crushed and/or milled to increase the reactive surface area of the feedstock and provide fresh reactive surfaces for the reaction with carbon dioxide. Because the reaction occurs only on the surfaces of the grains and within microcracks created by the crushing/milling process, it is essential to increase the available reaction surface area to the maximum extent possible in order to maximize the material reactivity.\| (2) The crushed and milled material may then be size sorted using sieves, gravity separation, air classifiers, to provide a final product with a mean grain size and overall grain size distribution which meets the engineering specifications of the coastal engineering project. In some cases, this process may be designed to exclude excessive fine-grained material and/or coarser particles, to produce an intermediate grain-size material which closely matches the size distribution of the native sediment in the geographic region receiving the carbon negative sand. As an alternative to preparing batches of CO2 - reactive components individually, it is also possible to presort the material into various predetermined size ranges and then select and/or blend from these preclassified separates to achieve an overall blend suitable for use in a specific project.\|In most cases or all cases, the CO2 - reactive component may be further modified via mixing non-reactive sediment in order to achieve a combination of texture, color, and density, and engineering properties suitable for use in coastal engineering products. To achieve this, a third step may be required:\| (3) The CO2-reactive mineral component may be blended with one or more chemicallyinert sand and sediment materials to achieve a predetermined ratio providing the specified properties. A list of common non-reactive feedstocks is provided in Table 2. Blends consisting of 1-50% reactive component may be most common, but other variations of this invention, higher or lower fractions of the reactive component may be used.\|Table 2. Potential feedstock materials for the non-reactive component of carbon-negative sand.Naturally Occurring Native Sediment at the Project Site: May include native sand, silt, clay, organic matter and gravelNaturally Occurring Rocks/Sediment: Silicate Beach Sand, Carbonate Beach Sand, Dredged Sediment, Crushed Sandstone, Crushed Limestone, Carbonate OoidsNaturally Occurring Minerals: Quartz, Feldspar, Aragonite, Calcite, Garnet, Magnetite, Hematite, Limonite, Ilmenite, Smectite, Chlorite, Biotite, Muscovite, Rutile, Zircon and Monazite\|[0066] The goal of blending the reactive- and non-reactive sediment components is to achieve a final bulk product meeting various regulatory, aesthetic and engineering requires including color, texture, grain size, density, cohesion, hardness, etc. To realize a blended mixture between the reactive and non-reactive components of the carbon-negative sand mixture, the individual components may either be brought together in advance, or in alternate embodiments, separately conveyed or placed onto the project site in such a manner to realize an appropriate mixture over the duration of the project (ie. mixing between components occurs via the physical motion of sediment driven by conveyors, heavy equipment, and/or waves and tides).\|[0067] Although enhanced silicate weathering may be implemented in some instances, none of the prior work has [8] recognized and provided methods for the manufacture of engineered carbon-negative materials with specific suitable colors, grainsize, density, and reactivity required to meet specific regulatory, aesthetic, and engineering requirement for coastal engineering. Moreover, [9] prior work has completely neglected the engineering of these specific attributes in order to create safe and successful materials for coastal engineering applications. [10] No existing material used in present coastal engineering applications provides additional public and ecological benefits due to CO2 capture, alkalinity generation, and the mitigation of ocean acidification. Likewise, [11] no prior approaches have realized the simultaneous benefits derived from manufacturing carbon-negative materials which are suitable for coastal engineering, thus providing a dual benefit of mitigating coastal erosion and sea level rise.\|Carbon Credits\|[0068] [5] In another aspect, the present disclosure provides systems and methods for measuring, recording and verifying (MRV) carbon removal as well as ecological effects of olivine sand in carbon removal over large coastal areas. Such measurements, recording, and verification of carbon removal may be performed using one or more remote sensors, protocols for the use of such sensors (benthic flux chambers), and algorithms to interpret the data obtained and derived from the sensor readings. The presently disclosed systems may be used to prove the dissolution of olivine and the subsequent capture of CO2 based on the dissolution of the olivine. In some cases, the systems and methods disclosed herein may be implemented to predict dissolution (e.g., by utilizing one or more models for simulating or predicting olivine dissolution at a target site).\|[0069] The present disclosure also provides software configured to calculate CO2 consumption and to measure/record/verify carbon removal. The software may be configured to determine CO2 consumption and/or carbon removal based on one or more sensor readings and/or one or more input parameters. The one or more input parameters may relate to, for example, the physical or chemical properties of the olivine used, the ratio of olivine to sand, the location in which the olivine is distributed, an amount of olivine distributed to a target site, or the manner/configuration in which the olivine is distributed (e.g., method of distribution, form of distribution, or spatial characteristics of the distribution). In some cases, the sensor readings may comprise measurements of alkalinity, pCO2, pH, and/or water temperature.\|[0070] In one aspect, the present disclosure provides methods and protocols for measuring, recording, and verifying (MRV) carbon removal (e.g., by way of coastal carbon capture using olivine). Referring to FIG. 12, the protocols may be submitted to independent, third-party entities (e.g., academics, institutions, etc.) for validation. Once validated, the protocols may be implemented by an individual or an entity. Additional third-party entities may ensure and confirm compliance. The individuals or entities implementing the MRV protocols may then submit the third-party verified, compliant methodologies to a carbon credit verifier, and an offset or a credit may be issued on a registry for sale in domestic and/or international markets.\|[0071] FIGs. 13 - 14 and FIG. 37 show a reaction representing the chemical mechanism by which coastal carbon capture can occur when olivine is introduced to a target site (e.g., by adding olivine sand to beaches and mixing the olivine sand with the native beach sand). For every 1 mol of olivine (which olivine may comprise or exhibit any of the physical or chemical properties or compositions described herein), 4 mols of carbon dioxide may be consumed or captured, and 4 mols of an alkaline material (bicarbonate or HCO3-) may be generated.\|[0072] FIGs. 15 - 20 show an environment comprising a first layer comprising seawater and a second layer comprising sediment and pore water. The sediment and pore water may span a dimension of about 10 centimeters (cm) or about 4 inches (in). The reactions shown in and described in relation to FIGs. 13 - 14 and FIG. 37 may drive the capture of carbon dioxide (e.g., CO2 in the atmosphere or in the seawater) and the release of magnesium, bicarbonate, and silicic acid. The rate of the overall reaction may be determined based on the fluxes associated with CO2 capture and the subsequent release of magnesium, bicarbonate, and silicic acid.\|[0073] In some non-limiting embodiments, one or more stirrers may be used to facilitate the carbon capture process (e.g., by physically mixing the seawater containing olivine sediments with the medium comprising the carbon dioxide). The medium may comprise a liquid medium (e.g., seawater) or a gaseous medium (e.g., air comprising atmospheric carbon dioxide). In some non-limiting embodiments, one or more valves may be used to control and regulate an outflow of any products of the reaction (e.g., the magnesium, bicarbonate, and/or silicic acid).\|[0074] FIG. 21A illustrates a plot of a change in concentration of an alkaline material in a flux chamber as a function of time when the olivine-based carbon capture reactions of the present disclosure are used. The alkalinity of the medium in which the alkaline material is present may gradually increase over time. In some cases, the alkalinity may increase by a factor of 1.1 to 10 or more over a period of 1 to 10 days. As shown in FIG. 21B, the alkalinity flux with olivine increases more rapidly over time than the alkalinity flux at a control site in which olivine is not introduced. The alkalinity flux may correspond to the slope of the lines shown in these plots, and may have units of change in concentration of the alkaline material per unit time.\|[0075] FIG. 22 shows an overview of the porewater method for determining flux of an alkaline material that is produced. The porewater method may be based on Fick's first law of diffusion. The flux of the alkaline material may be determined based on a diffusion coefficient (representing area per unit time) and a dC/dZ value (representing a change in concentration or amount of substance per unit volume, as a function of position or dimensional length). With olivine present in porewater, a larger flux may be observed (steeper slope and bigger flux), whereas when olivine is not present, a smaller flux is observed (shallower slope and smaller flux).\|[0076] FIG. 23 shows a shrinking core model comprising a transformed volume and an untransformed volume of an exemplary olivine particle. The shrinking core model may be represented by X = 1 - [1 - R/(ρ∗d))∗t]^3, where X is the fraction of olivine reacted, R is a function of pH and temperature, p is molar density, d is starting diameter, and t represents time. One assumption for this model is that the particles are a perfect sphere.\|[0077] FIG. 24 shows dissolution rates for olivine having various grain sizes. The fraction of olivine reacted over time may increase more rapidly for olivine particles having smaller grain sizes. For example, for olivine with a 30 micrometer grain size, 10% of the olivine may react within 3 years, 50% of the olivine may react within 18 years, and 90% of the olivine may react within 47 years. In contrast, for olivine with a 64 micrometer grain size, 10% of the olivine may react within 6 years, 50% of the olivine may react within 39 years, and 90% of the olivine may react within 101 years. The rates shown generally correspond to static dissolution rates based on inorganic chemical processes, and may not include acceleration of weathering due to wave energy and biotic processes. The systems and methods of the present disclosure may be implemented to optimize dissolution rates by (1) inducing or imparting wave energy with a specific characteristic (e.g., periodicity, intensity, motion path, etc.) and/or (2) modifying the biotic processes used to enhance olivine dissolution.\|[0078] FIG. 25 shows an exemplary modeling approach for particle distribution. In one step, the modeling approach may comprise simulating grains to match a desired particle size distribution. The modeling approach may further comprise shrinking each particle over a time period (e.g., to simulate dissolution or erosion of one or more portions or layers of each particle), and thereafter summing the total mass of the particles and/or the total amount dissolved or eroded at various time points in order to determine the fraction of mass remaining as a function of time.\|[0079] FIG. 26 shows dissolution rates for different mixtures of olivine having different mean grain sizes. In general, olivine mixtures with smaller mean grain sizes may have a shorter half-life (i.e., a shorter time period for half of the olivine mixture to dissolve under a particular set of conditions).\|[0080] FIG. 27 shows the impact of temperature and pH on half-life. In some cases, the half-life for olivine dissolution may decrease as temperature increases. In some cases, the half-life for olivine dissolution may increase as pH increases. In some embodiments, the systems and methods disclosed herein may be implemented to optimize temperatures and pHs for dissolution environments to shorten the half-life for olivine dissolution. In other embodiments, the systems and methods disclosed herein may be implemented to identify candidate locations with optimal temperatures and pHs for olivine dissolution environments to shorten the half-life for olivine dissolution.\|[0081] The systems and methods disclosed herein may be configured or implemented to overcome challenges relating to spatial and temporal heterogeneity, low signal/noise ratios due to slow dissolution of olivine, and variation in secondary mineral product generation. The systems and methods disclosed herein may also help to overcome verification challenges such as, for example, objective criteria for acceptance and verification of carbon credit sales, and how to influence such criteria to adapt them to coastal weathering processes.\|[0082] The present disclosure provides methods for performing MRV (i.e., the measurement, recording, and verification) of carbon capture and/or olivine dissolution. In some cases, the methods may comprise establishing a treatment site and a reference or baseline site. The methods may further comprise measuring alkalinity fluxes and/or other parameters at a network of discrete locations. In some cases, this may be repeated over time as olivine dissolves over a series of time points. The methods may further comprise interpolating in time and space to determine an overall dissolution rate across an area or a volume of the site. In some cases, the overall dissolution rate across the site may be determined in part using a numerical reaction transport model that provides a fit to the measured data.\|[0083] FIG. 28 shows examples of temporal factors and spatial factors that can vary for coastal ecosystems, many of which are extremely dynamic. Temporal factors may include, for example, diurnal factors (i.e., day/night variations), tides, seasonality, temperature, weather, and/or waves. Spatial factors may include, for example, position and hydrodynamics, depth, tides, sediment type, grain size, sediment organic carbon content, and/or bottom cover (e.g., sea grass, rocks, coral, etc.).\|[0084] In some cases, the methods disclosed herein may comprise assessing or evaluating temporal heterogeneity by measuring depth, temperature, salinity, pH, turbidity, chlorophyll concentrations, and/or dissolved oxygen concentrations over time. FIG. 29 shows plots of temporal heterogeneity of various characteristics for a target site, including depth, salinity, turbidity, temperature, dissolved, oxygen, and pH. In some cases, the target site for olivine distribution and dissolution may be chosen based on temporal heterogeneity relative to other candidate or baseline/reference sites.\|[0085] As shown in FIGs. 30 - 32, in some cases, the methods disclosed herein may comprise calculating alkalinity fluxes and measuring dissolution rates of olivine to secure carbon credits. Alkalinity fluxes induced by olivine may be determined by discerning changes in alkalinity fluxes due to olivine from other natural background fluxes. In some cases, other fluxes attributable to olivine, such as dissolved inorganic carbon (DIC) fluxes and fluxes of pCO2, may be determined based on a comparison of measured fluxes to natural background fluxes. The fluxes attributable to olivine dissolution and/or the natural background fluxes may be space and time dependent. Such variations over space and time may be simulated, modeled, tracked, and/or measured to ensure accurate calculation of fluxes attributable to olivine, as opposed to natural background fluxes.\|[0086] In another aspect, the present disclosure provides various methods for accounting for heterogeneity for MRV. FIG. 33 shows a summary of the MRV approaches described below at different scales of cost and complexity.\|[0087] Approach 1 - In some cases, the methods may involve using the shrinking core model described elsewhere herein for an approximate rate of dissolution. The dissolution rate and CO2/olivine ratio may be assumed or approximated.\|[0088] Approach 2 - Alternatively, mesocosm experiments may be utilized to determine regional olivine dissolution rates. In cases where olivine is deployed in a target site (e.g., a mesocosm or the natural environment), olivine tracers may be used to track olivine dissolution in order to model and refine in situ weathering rates. The present disclosure provides systems and methods to track the movement of olivine grains in a target site. The systems and methods of the present disclosure may be implemented to track olivine transport in a target site based on or using, for example, trace metal content, fluorescent dyes, and/or olivine-specific spectral properties. This may be a relatively inexpensive process that can be set up prior to obtaining regulatory permits. Further, this approach may be initially tested using a sealed, recirculating design that is configured to maintain and control spatiotemporal heterogeneity and further allow for temperature and/or lighting control.\|[0089] Approach 3 - In some cases, the mesocosm-based approaches described herein may be augmented with field data (e.g., in situ data obtained manually or automatically using one or more sensors). The data obtained using the one or more sensors (which one or more sensors may comprise any of the sensors described herein or any other sensors for obtaining any of the measurements referred to herein) may provide additional information to better quantify and track spatial and/or temporal variations in environmental conditions or parameters relating to olivine dissolution and coastal carbon capture.\|[0090] Approach 4 - In some cases, a numerical model may be constructed that allows for accurate simulation of spatial and temporal variations in background fluxes and olivine dissolution rates. This can help to correct for time and space dependent variations, and allow for the use of sparse observations or other information or data at discrete points (e.g., points in time and/or points in space) to calibrate, verify, and validate the model. The model may be built and implemented for one or more a priori simulations.\|[0091] In cases where olivine is deployed in the natural environment, olivine tracers may be used to track olivine dissolution in order to estimate, predict, model, and refine in situ weathering rates. The present disclosure provides systems and methods for tracking the movement or transport of olivine grains in the natural environment (e.g., in a target site in which the olivine is provided or introduced). The systems and methods of the present disclosure may be implemented to track olivine transport based on or using, for example, trace metal content, fluorescent dyes, and/or olivine-specific spectral properties. The trace metal content, the movement or dispersion of fluorescent dyes, and/or the olivine-specific spectral properties may be detected and tracked using any of the sensors described herein.\|[0092] FIG. 34 illustrates various examples of reaction-transport modeling studies that may be used to simulate sediment porewater profiles, solid-phase chemistry, and benthic fluxes. The simulations and studies may be tailored to project requirements, and can take into account secondary clay mineralogy and Cr and Ni speciation and cycling. The plots shown in FIG. 34 illustrate an exemplary numerical simulation of alkalinity profile and the effects of spreading a 2 centimeter (cm) thick layer of pure olivine sand on a beach sediment. In some cases, the alkalinity flux across the sediment-water interface may be monitored by (1) constructing biogeochemical models of olivine dissolution in sediments, (2) validating model performance using field measurements of sediment-water alkalinity flux (and other carbonate parameters), and (3) calculating CO2 capture, storage, or sequestration (by weight or volume) based on the thermodynamics of air-sea CO2 exchange.\|[0093] The systems and methods disclosed herein may be implemented using one or more sensors capable of measuring at optimal spatial and temporal resolutions. The sensors may obviate the need to use traditional, manual geochemical methods, which require labor intensive field sampling and returning of samples to labs for analysis and can involve significant costs. FIG. 35 shows various examples of sensors that can be used for MRV, including sensors configured to measure temperature, salinity, pH, pCO2, DIC, alkalinity, and/or wave impacts on sand. In some cases, a solid state sensor for simultaneous measurement of total alkalinity and pH of seawater (including seawater that does or does not comprise olivine) may be used. In some embodiments, a plurality of sensors for MRV may be deployed on a single system. In other embodiments, a plurality of sensors for MRV may be deployed on multiple separate systems. Additional examples of sensors are shown in FIG. 36, including silicate sensors, alkalinity sensors, CTDO sensors, Cytochips, dissolved inorganic carbon sensors, and nitrate sensors. In some cases, a 29Si isotopic tracer can be used to track olivine dissolution and simultaneous precipitation of secondary clays and carbonate phases. This can allow separation of total and net silicate dissolution.\|[0094] In some cases, the impacts of physical wave-driven weathering on beach sand and olivine dissolution may be measured or simulated. In some cases, this may involve measuring and analyzing 2-phase (i.e., sand-water) flow in the benthic boundary layer of a breaking wave. This may be modeled numerically or physically (e.g., using wave tanks). In some cases, specialized sensors for measuring turbulent energy dissipation (e.g., in a lab or directly on a beach) may be utilized to measure impacts of physical wave-driven weathering.\|[0095] FIG. 38 illustrates an approach to measuring CO2 removal that is enabled by way of the reactions shown in FIG. 37. In some cases, it may not be feasible to monitor the air to sea CO2 flux. Measuring air-sea CO2 fluxes can be challenging because the olivine dissolution signal is strongly muted by dilution with open ocean seawater. For instance, a 1 cm thick layer of olivine dissolving in 5 meters of water in a bay with a 4-hour residence time implies a ~ 1.3 µM increase in water column alkalinity. Measuring net CO2 flux can also be complicated by extreme seasonal and diurnal variations in ΔPCO2air-sea due to changes in local photosynthesis and respiration. Accordingly, in some embodiments, the systems and methods disclosed herein may be implemented to monitor alkalinity flux across the sediment-water interface.\|[0096] In some cases, the models described herein (which models may be generated for specific sites) may undergo validation. Such validation may involve determining olivine abundance, spatial distribution, and dissolution rates at one or more reference points in space or time. In some cases, the reference points may be arranged in a grid pattern. Validation may further involve crossvalidating measured and modeled alkalinity fluxes and olivine dissolution at reference points, and calculating alkalinity flux for a region or a project based on (i) a known mass or volume of olivine deployed and (ii) validated site-specific modeling. The models may be validated using one or more sensor measurements as described elsewhere herein. Once validated, the models may be used to determine or predict olivine dissolution, reaction fluxes, and/or carbon sequestration. In some cases, the models may be updated or refined based on additional sensor measurements captured over a period of time. In some cases, the models may be revalidated based on additional sensor measurements.\|[0097] FIG. 39 illustrates an approach to calculating CO2 sequestration from alkalinity flux based on an expression of how water DIC storage changes as a function of increasing alkalinity. Seawater carbonate chemistry may be controlled by pCO2, pH, DIC, and alkalinity. An isocapnic quotient may be computed based on a change in alkalinity relative to a change in DIC, at fixed conditions for pCO2, temperature, and salinity. In some cases, a 1 micromol increase in alkalinity may yield a 0.78-0.93 micromol DIC increase, which means that for every one ton of forsterite provided to a target site, 0.97 to 1.16 tons of CO2 can be stored as marine DIC.\|[0098] FIG. 40 illustrates a plot showing seawater age and the depth below sea water level of the Atlantic Ocean as a function of latitude (degrees North). CO2 capture via ocean alkalinization requires that the enhanced alkalinity water mass achieves equilibrium with atmospheric pCO2. The precise timescale for pCO2 equilibrium (~ 4 months) and DIC adjustment (~4 years) depends on the Revelle factor (Jones et al. 2014). The time scale for air-sea equilibration is considerably shorter than the time scale for olivine dissolution (~ 10 - 100 year) and approximately similar to the transit time distribution of mixed layer and subtropical mode water (- 10 - 40 years). This means that the surface DIC reservoir can achieve quasi-steady equilibrium throughout equatorial and subtropical regions most suitable for coastal enhanced weather.\|[0099] FIG. 41 illustrates an exemplary CEW life cycle analysis. The life cycle may comprise mining and/or extracting olivine, grinding the olivine to approximately 400 micrometer grain sizes (or less), transporting the olivine to one or more target sites, and spreading the olivine at the target sites. In some cases, the life cycle may be at least about 89% efficient, and can enable sequestration of at least about 5 to 20 times more CO2 than the amount of CO2 emitted during mining, grinding, transportation, and/or spreading of olivine.\|[0100] FIG. 42 illustrates an example of a carbon payback period that can be realized using the methods and systems disclosed herein. In some cases, the break even payback period may occur at approximately 4 years, assuming the following:\| Grainsize: LE45 (d50: 365 µm)\| Temp: 25 °C\| pH: 8\| Embedded emissions: 110 tons CO2 / 1000 tons olivine\| Absorption efficiency: 3 moles ALK / mole olivine\| Dissolution constant: Log(r) = - 8.75 (can vary depending on pH/temp)\|[0101] FIG. 43 illustrates various plots showing exemplary olivine dissolution kinetics for olivine particles having different grain sizes. Dissolution time may decrease as olivine particle sizes decrease. The particle dissolution characteristics may be predicted or simulated using a shrinking core model and one or more laws, equations, or principles governing olivine dissolution rates. In some cases, the shrinking core model may be modified to permit the simulation of dissolution for realistic, commercially-available grain size distributions. The models described herein may be generated by modifying initial diagenesis models to incorporate olivine dissolution kinetics that correspond to the shrinking core model. The models may include and/or account for full carbonate chemistry (e.g., DIC, ALK, pCO2, pH, carbonate precipitation/dissolution) as well as biogeochemical processes (including aerobic and anaerobic respiration, formation of Fe/Mn oxides, pyrite, sulfide oxidation, etc).\|[0102] In some instances, secondary carbonate precipitation as shown in FIG. 44 can impact CO2 capture efficiency. Secondary carbonate precipitation may change the reactions described herein such that for every 1 mol of olivine introduced to a target environment, 2 moles of CO2 are consumed and 0 moles of alkalinity are generated. This can result in a 50% reduction in CO2 capture efficiency. The systems and methods disclosed herein may be implemented to minimize or reduce secondary carbonate precipitation. The rate of carbonate precipitation can be strongly controlled by local variations in geochemistry and biogenic calcification. In some cases, alkalinity export can be the dominant process occurring in sediments, and once mixed into the water column, consumption of alkalinity can be low given the long residence time of DIC and ALK in seawater.\|[0103] In some instances, secondary clay formation as shown in FIG. 45 can impact CO2 capture efficiency. Secondary clay formation may change the reactions described herein such that for every 1 mol of olivine, 8/3 moles of CO2 are consumed and 8/3 moles of alkalinity are generated. This can result in a 33% reduction in CO2 capture efficiency. The systems and methods disclosed herein may be implemented to minimize or reduce such secondary clay formation.\|[0104] In a related aspect, the present disclosure provides systems and methods for simulating a target site or environment. This can allow the study of olivine dissolution rates in a controlled environment, intermediate between lab and field conditions. Such systems and methods may be implemented to determine and/or monitor olivine dissolution rates, porewater geochemistry, or benthic flux measurements, study impacts of temperature on olivine dissolution and respiration, track impacts on seawater pH and other water chemistry, monitor ecological responses and air-sea water gas CO2 fluxes, track the fate, transport, and bioaccumulation of Cr and Ni, track the formation of secondary weathering products (e.g., Chrysotile, Carbonates, Clays), and monitor the impacts of olivine-based CO2 sequestration processes on benthic invertebrates/meiofauna.\|[0105] In some embodiments, the MRV methods and protocols disclosed herein may be adapted or adjusted for different types of olivine or for different target sites for olivine distribution. In such cases, the models used to predict or determine olivine dissolution, reaction fluxes, and/or carbon sequestration may be adjusted based on characteristics of the particular olivine/sand mixture used, the target site, and/or one or more sensor readings or measurements obtained in situ.\|Carbon Removal Prediction\|[0106] [6] In another aspect, the present disclosure provides systems and methods for predicting rates of carbon removal at specific sites. Such predictions may be based on, for example, data corresponding to measurement of changes in alkalinity, pCO2, pH, and/or water temperature. The predictions may be generated using algorithms and software interpreting such data. The algorithms and software may be implemented by way of one or more models that can be generated based on the MRV data obtained using various sensors as described elsewhere herein.\|[0107] In some embodiments, the predicted rates of carbon removal may be used to further optimize the carbon capture process. For instance, the predicted rates may be used to optimize the properties of the olivine sand, the preparation of the olivine sand, and/or the operation or the configuration of the reactor.\|Shipping and Deployment of Olivine\|[0108] [7] In another aspect, the present disclosure provides systems and methods for shipping and deploying olivine. In some cases, the shipping and deployment of olivine may be performed using a device for distributing carbon negative sand in shallow marine environments. The device may be, for example, a spreading device for spreading the olivine in a desired or optimal manner at a target site (e.g., a beach of interest).\|[0109] In some cases, the methods of the present disclosure may comprise determining whether one or more dredging modifications are needed in order to optimally distribute the carbon negative sand. Such determination may be based on one or more sensor readings and/or information about the target site in which the carbon negative sand is to be distributed.\|[0110] In some cases, the olivine may be processed before shipping to facilitate shipping and distribution of the olivine. For instance, the olivine may be modified to enable transportation of ultra-fine material (e.g., for reduction of liquefaction or capsizing risk.\|[0111] In some embodiments, various types and forms of maritime emissions reduction technology (e.g., an on-board olivine reactor driven by ship engine using ballast water) may be implemented. In some cases, bulk carrier direct deployment technology and related modifications (e.g., open sea distribution for in situ CEW) may be utilized. In some cases, grain washing and liquid alkalinity systems may be used for pre-deployment reduction of turbidity. In some cases, global logistics software may be used to mobilize idle maritime assets for carbon removal projects.\|[0112] FIG. 9 schematically illustrates an example of a system that may be used to deploy olivine for coastal nourishment. The system may comprise, for example, a split hulled hopper barge. In some cases, olivine may be mined and milled into carbon negative sand. Thereafter, the olivine may be loaded and shipped on dry bulk carriers to designated ports. The olivine may then be loaded into one or more split hulled hopper barges. In some embodiments, the barges may be linked together and towed to designated deployment sites. Once the barges are positioned at or near the designated deployment sites, the bottom of the barges may be configured to open in order to deploy the olivine. In some cases, sediment transport modeling may be used to predict where the olivine will move and/or in what directions the olivine will disperse.\|[0113] In a further aspect, the present disclosure provides a method and process for conducting carbon neutral and carbon negative dredging operations. The method and process of conducting dredging operations may be either net neutral or net negative with respect to atmospheric greenhouse gas emissions. To achieve this, dredged sediment may be mixed with one or more types of carbon negative sand, as described elsewhere herein. The methods and processes described herein may be adapted for any type of construction activity, including land-based construction activities.\|[0114] The dissolution of carbon negative sand may effect the conversion of gaseous and dissolved carbon dioxide into dissolved bicarbonate and carbonate ions, thereby increasing the capacity of fresh and salt water to store additional carbon in a dissolved state. When present as dissolved bicarbonate and carbonate ions, rather than carbon dioxide, these compounds may no longer contribute to climate change and can act to counter the effect of ocean acidification.\|[0115] In order to reduce, neutralize, or negate carbon dioxide emissions which occur during the combustion of fossil fuels during conventional dredging operations, a predefined ratio of carbon negative sand may be mixed with the dredging spoils in order to [1] result in the net capture of a specified amount of carbon dioxide and [2] ensure that the dredged sediments meet engineering and regulatory requirements for disposal or beneficial reuse. Blends consisting of 1-50% reactive carbon negative component may be most common, but in other variations, higher or lower fractions of the carbon negative component may be used.\|[0116] In order to mix carbon negative sand with dredged materials, several different approaches may be used depending on the type of dredging operation and intended fate of the dredged material. During cutterhead dredging operations, pump-out hopper dredging, and other approaches where dredged material is conveyed via a hydrologic slurry, the carbon negative sand may be directly mixed with the dredge spoils by injecting the carbon negative sand into the slurry pipeline. When using trailing suction hopper dredges, carbon negative sand may be mixed within a sediment hopper or barge prior to discharge. As an alternative, carbon negative sand may be directly placed at the sediment destination in the specified quantity and allowed to mix with the dredge spoils via the action of wind, waves, tides, and currents.\|[0117] Whereas traditional dredging operations consume large quantities of fuel fuels and emit correspondingly large quantities of greenhouse gasses, the method and process described here may allow dredging operations to be conducted in a way that is carbon neutral or even carbon negative over the lifetime of the project. This method and process provides significant advantages, allowing dredging operators to (i) mitigate carbon dioxide emissions on behalf of themselves or their clients, (ii) avoid emissions caps and taxes, and (iii) operate in jurisdictions which impose voluntary or involuntary restrictions on greenhouse gas emissions.\|Carbon-removing marine landfill cap\|[0118] In another aspect, the present disclosure provides carbon-removing marine landfill caps, processes for making the same, and processes for quantifying carbon capture from carbon-removing marine landfill caps. Marine landfills may serve as long-term, seafloor placement areas for unwanted construction debris, dredging materials, and toxic pollutants. Currently, marine landfills are often "capped" with non-toxic clay or sand or other similar materials to prevent contamination of overlying seawater and allow marine life to thrive in previously environmentally damaged areas. By using carbon-removing sand wholly, or as a constituent of, marine landfill caps, these sites can serve as climate change mitigation locales and further encourage the regeneration of environmentally damaged areas through the production of bicarbonate (alkalinity) which offsets ocean acidification and is beneficial for marine life.\|[0119] The process of making and deploying carbon-removing marine landfill cap differs from traditional marine landfill cap because 1) the depth (thickness) of carbon-removing cap sand 2) grain size distribution of carbon-removing cap sand, and 3) possible blend of carbon-removing cap and standard cap must be optimized to 1) prevent release of toxic pollutants and similar while allowing for sufficient permeability so that the carbon-removing sand will capture carbon over time and in particular not saturate sand porewaters such that the carbon removal reaction slows or stops. To achieve these objectives, a carbon-removing marine landfill cap may be deployed wholly as a cap, applied as a single mixture of carbon-removing cap to regular cap sand, or applied in layers where the percentage of carbon-removing cap sand to regular cap sand changes with depth, or the grain size distribution of carbon-removing cap and/or standard cap changes with depth. In all circumstances the carbon capture rates may vary with depth. In some cases, the carbon capture rate may be determined based on analytical measurements and sensor measurements from a particular site, fit to a global model. In some embodiments, the appropriate deployment technique described above may be a function of local wave climate, ecology (bioturbation), seawater temperature, landfill material, and an LCA (life cycle analysis) as the CO2 emitted to deploy the carbon-removing cap must be accounted for to insure the cap is, indeed, carbon-removing.\|Green Hydrogen\|[0120] [8] In another aspect, the present disclosure provides systems and methods for generating and using green hydrogen. As used herein, the term "green hydrogen" may refer to hydrogen that is produced from renewable energy sources and/or low-carbon power sources. The green hydrogen may be used as fuel for fuel cells or internal combustion engines. In some cases, the green hydrogen may be generated based on one or more products or reactants used to drive the CO2 capture and sequestration reactions/methods described elsewhere herein.\|Computer Systems\|[0121] In an aspect, the present disclosure provides computer systems that are programmed or otherwise configured to implement methods of the disclosure, e.g., any of the subject methods for processing and distributing olivine. FIG. 10 shows a computer system 1001 that is programmed or otherwise configured to implement a method for olivine processing and distribution. The computer system 1001 may be configured to, for example, (i) identify a target site, (ii) optimize one or more procedures for processing olivine to yield favorable properties or characteristics for the olivine, based on the target site identified, and (iii) coordinate transportation of the olivine to the target site. The computer system 1001 can be an electronic device of a user or a computer system that is remotely located with respect to the electronic device. The electronic device can be a mobile electronic device.\|[0122] The computer system 1001 may include a central processing unit (CPU, also "processor" and "computer processor" herein) 1005, which can be a single core or multi core processor, or a plurality of processors for parallel processing. The computer system 1001 also includes memory or memory location 1010 (e.g., random-access memory, read-only memory, flash memory), electronic storage unit 1015 (e.g., hard disk), communication interface 1020 (e.g., network adapter) for communicating with one or more other systems, and peripheral devices 1025, such as cache, other memory, data storage and/or electronic display adapters. The memory 1010, storage unit 1015, interface 1020 and peripheral devices 1025 are in communication with the CPU 1005 through a communication bus (solid lines), such as a motherboard. The storage unit 1015 can be a data storage unit (or data repository) for storing data. The computer system 1001 can be operatively coupled to a computer network ("network") 1030 with the aid of the communication interface 1020. The network 1030 can be the Internet, an internet and/or extranet, or an intranet and/or extranet that is in communication with the Internet. The network 1030 in some cases is a telecommunication and/or data network. The network 1030 can include one or more computer servers, which can enable distributed computing, such as cloud computing. The network 1030, in some cases with the aid of the computer system 1001, can implement a peer-to-peer network, which may enable devices coupled to the computer system 1001 to behave as a client or a server.\|[0123] The CPU 1005 can execute a sequence of machine-readable instructions, which can be embodied in a program or software. The instructions may be stored in a memory location, such as the memory 1010. The instructions can be directed to the CPU 1005, which can subsequently program or otherwise configure the CPU 1005 to implement methods of the present disclosure. Examples of operations performed by the CPU 1005 can include fetch, decode, execute, and writeback.\|[0124] The CPU 1005 can be part of a circuit, such as an integrated circuit. One or more other components of the system 1001 can be included in the circuit. In some cases, the circuit is an application specific integrated circuit (ASIC).\|[0125] The storage unit 1015 can store files, such as drivers, libraries and saved programs. The storage unit 1015 can store user data, e.g., user preferences and user programs. The computer system 1001 in some cases can include one or more additional data storage units that are located external to the computer system 1001 (e.g., on a remote server that is in communication with the computer system 1001 through an intranet or the Internet).\|[0126] The computer system 1001 can communicate with one or more remote computer systems through the network 1030. For instance, the computer system 1001 can communicate with a remote computer system of a user (e.g., an end user performing or monitoring the processing and/or the transportation or distribution of the olivine). Examples of remote computer systems include personal computers (e.g., portable PC), slate or tablet PC's (e.g., Apple® iPad, Samsung® Tab), telephones, Smart phones (e.g., Apple® iPhone, Android-enabled device, Blackberry®), or personal digital assistants. The user can access the computer system 1001 via the network 1030.\|[0127] Methods as described herein can be implemented by way of machine (e.g., computer processor) executable code stored on an electronic storage location of the computer system 1001, such as, for example, on the memory 1010 or electronic storage unit 1015. The machine executable or machine readable code can be provided in the form of software. During use, the code can be executed by the processor 1005. In some cases, the code can be retrieved from the storage unit 1015 and stored on the memory 1010 for ready access by the processor 1005. In some situations, the electronic storage unit 1015 can be precluded, and machine-executable instructions are stored on memory 1010.\|[0128] The code can be pre-compiled and configured for use with a machine having a processor adapted to execute the code, or can be compiled during runtime. The code can be supplied in a programming language that can be selected to enable the code to execute in a pre-compiled or ascompiled fashion.\|[0129] Aspects of the systems and methods provided herein, such as the computer system 1001, can be embodied in programming. Various aspects of the technology may be thought of as "products" or "articles of manufacture" typically in the form of machine (or processor) executable code and/or associated data that is carried on or embodied in a type of machine readable medium. Machine-executable code can be stored on an electronic storage unit, such as memory (e.g., read-only memory, random-access memory, flash memory) or a hard disk. "Storage" type media can include any or all of the tangible memory of the computers, processors or the like, or associated modules thereof, such as various semiconductor memories, tape drives, disk drives and the like, which may provide non-transitory storage at any time for the software programming. All or portions of the software may at times be communicated through the Internet or various other telecommunication networks. Such communications, for example, may enable loading of the software from one computer or processor into another, for example, from a management server or host computer into the computer platform of an application server. Thus, another type of media that may bear the software elements includes optical, electrical and electromagnetic waves, such as used across physical interfaces between local devices, through wired and optical landline networks and over various air-links. The physical elements that carry such waves, such as wired or wireless links, optical links or the like, also may be considered as media bearing the software. As used herein, unless restricted to non-transitory, tangible "storage" media, terms such as computer or machine "readable medium" refer to any medium that participates in providing instructions to a processor for execution.\|[0130] Hence, a machine readable medium, such as computer-executable code, may take many forms, including but not limited to, a tangible storage medium, a carrier wave medium or physical transmission medium. Non-volatile storage media including, for example, optical or magnetic disks, or any storage devices in any computer(s) or the like, may be used to implement the databases, etc. shown in the drawings. Volatile storage media include dynamic memory, such as main memory of such a computer platform. Tangible transmission media include coaxial cables; copper wire and fiber optics, including the wires that comprise a bus within a computer system. Carrier-wave transmission media may take the form of electric or electromagnetic signals, or acoustic or light waves such as those generated during radio frequency (RF) and infrared (IR) data communications. Common forms of computer-readable media therefore include for example: a floppy disk, a flexible disk, hard disk, magnetic tape, any other magnetic medium, a CD-ROM, DVD or DVD-ROM, any other optical medium, punch cards paper tape, any other physical storage medium with patterns of holes, a RAM, a ROM, a PROM and EPROM, a FLASH-EPROM, any other memory chip or cartridge, a carrier wave transporting data or instructions, cables or links transporting such a carrier wave, or any other medium from which a computer may read programming code and/or data. Many of these forms of computer readable media may be involved in carrying one or more sequences of one or more instructions to a processor for execution.\|[0131] The computer system 1001 can include or be in communication with an electronic display 1035 that comprises a user interface (UI) 1040 for providing, for example, a portal for a user to monitor the processing and/or the transportation or distribution of the olivine. The portal may be provided through an application programming interface (API). A user or entity can also interact with various elements in the portal via the UI. Examples of UI's include, without limitation, a graphical user interface (GUI) and web-based user interface.\|[0132] Methods and systems of the present disclosure can be implemented by way of one or more algorithms. An algorithm can be implemented by way of software upon execution by the central processing unit 1005. For example, the algorithm may be configured to identify a target site and optimize a procedure for processing the olivine based on the properties or the characteristics of the target site.\|[0133] While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. It is not intended that the invention be limited by the specific examples provided within the specification. While the invention has been described with reference to the aforementioned specification, the descriptions and illustrations of the embodiments herein are not meant to be construed in a limiting sense. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. Furthermore, it shall be understood that all aspects of the invention are not limited to the specific depictions, configurations or relative proportions set forth herein which depend upon a variety of conditions and variables. It should be understood that various alternatives to the embodiments of the invention described herein may be employed in practicing the invention. It is therefore contemplated that the invention shall also cover any such alternatives, modifications, variations or equivalents. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby.	Family Number\|(104628663)\|104628663\|Advantages / Prev. Drawbacks\|(EP4166641 A1)\|The systems and methods of the present disclosure enable the acceleration of Earth's natural carbon removal method of rock weathering, through the extraction, processing (e.g., crushing and/or grinding), and transportation of volcanic mineral olivine to coastlines for dispersal or distribution.\|Independent Claims\|(EP4166641 A1)\| (...) (a) generating one or more models for determining or predicting olivine dissolution, carbon sequestration, or one or more reaction fluxes associated with a dissolution of olivine in a target environment; (...) (d) using the one or more validated and/or updated models to determine or predict (i) olivine dissolution, (ii) carbon sequestration, and (iii) the one or more reaction fluxes in the target environment.\|	Biotechnology	C12M-025/16\|C12M-043/04\|Y02C-020/40		C12M-025/16\|C12M-043/04\|Y02C-020/40	C12M-001/12	C12M-001/12			GB2636851	GB2636851 108540140 WHO=Examiner SELF=N				XP055953515; XP086406848; XP055953378; XP028640436; XP055811339	(EP4166641)\|Applicant references\|-GERRITS RUBEN: "An experimental study of fungal olivine weathering", 1 January 2019 (2019-01-01), XP055953515, Retrieved from the Internet <URL:https://opus4.kobv.de/opus4-bam/files/48825/Dissertation-Ruben%20Gerrits-final.pdf> [retrieved on 20220822], DOI: 10.17169/refubium-2880\|-GERRITS R ET AL: "High-resolution imaging of fungal biofilm-induced olivine weathering", CHEMICAL GEOLOGY, ELSEVIER SCIENCE PUBLISHER B.V., AMSTERDAM, NL, vol. 559, 24 September 2020 (2020-09-24), XP086406848, ISSN: 0009-2541, [retrieved on 20200924], DOI: 10.1016/J.CHEMGEO.2020.119902\|-TORRES MARK A. ET AL: "Microbial Acceleration of Olivine Dissolution via Siderophore Production", PROCEDIA EARTH AND PLANETARY SCIENCE, vol. 10, 1 January 2014 (2014-01-01), AMSTERDAM, NL, pages 118 - 122, XP055953378, ISSN: 1878-5220, Retrieved from the Internet <URL:https://www.researchgate.net/profile/Kenneth-Nealson/publication/265089771_Microbial_Acceleration_of_Olivine_Dissolution_via_Siderophore_Production/links/546caa6b0cf24b753c628dad/Microbial-Acceleration-of-Olivine-Dissolution-via-Siderophore-Production.pdf> DOI: 10.1016/j.proeps.2014.08.041\|-MOROZ LYUBA V ET AL: "Space weathering of silicate regoliths with various FeO contents: New insights from laser irradiation experiments and theoretical spectral simulations", ICARUS, ACADEMIC PRESS, SAN DIEGO, CA, US, vol. 235, 24 March 2014 (2014-03-24), pages 187 - 206, XP028640436, ISSN: 0019-1035, DOI: 10.1016/J.ICARUS.2014.03.021\|-KÖHLER PETER ET AL: "Environmental Research Letters LETTER @BULLET OPEN ACCESS Geoengineering impact of open ocean dissolution of olivine on atmospheric CO 2 , surface ocean pH and marine biology", ENVIRON. RES. LETT, 21 January 2013 (2013-01-21), pages 14009 - 9, XP055811339, Retrieved from the Internet <URL:https://iopscience.iop.org/article/10.1088/1748-9326/8/1/014009/pdf> [retrieved on 20210608]\|	LAPSED	(EP4166641)\|LAPSED	DEAD	(EP4166641)\|DEAD	(EP4166641)\|LEGAL DETAILS FOR EP4166641\|Actual or expected expiration date=2023-10-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-02-17\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP22157366\|Application date=2022-02-17\|Standardized application number=2022EP-0157366\|Event publication date=2023-03-17\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2023-03-17\|Event code=EP/STAAPB\|Event group=Examination events\|The application has been published\|Original code: STAA\|Event publication date=2023-04-19\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP4166641\|Publication stage code=A1\|Publication date=2023-04-19\|Standardized publication number=EP4166641\|Event publication date=2023-04-19\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2024-02-16\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2024-03-20\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2023-10-20	(EP4166641)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4166641)\|Extension States: ME, BA\|(EP4166641)\|Validation States: MA, MD, TN, KH		https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=VCVyqWEeIcCG2afaYUkNFqCa4vFyxJplNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP0000000010242243&ekey=2092&xpn=EP4166641&kind=A1	https://register.epo.org/application?number=EP22157366	https://permalink.orbit.com/RenderStaticFirstPage?XPN=f6P6m2tQ6MEuw56Xk6cpNXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(EP4166641)\|US	(EP4166641)\|NAME=Project Vesta, PBC 584 Castro St 2054 , CITY=San Francisco, CA 94114 , COUNTRY=US , REG=101937721	(EP4166641)\|GB	(EP4166641)\|NAME=Hamer, Christopher K. Mathys & Squire , CITY=The Shard32 London Bridge StreetLondon SE1 9SG , COUNTRY=GB , REG=100052783	(EP4166641)\|US; US; US; US; US; US; US	(EP4166641)\|NAME=ROMANIELLO, Stephen Justin, CITY=San Francisco, 94114, COUNTRY=US \|NAME=LEY, Brian David, CITY=San Francisco, 94114, COUNTRY=US \|NAME=ANDREWS, Margaret Grace, CITY=San Francisco, 94114, COUNTRY=US \|NAME=WALWORTH, Nathan Gerard, CITY=San Francisco, 94114, COUNTRY=US \|NAME=ISHOEY, Thomas, CITY=San Francisco, 94114, COUNTRY=US \|NAME=GREEN, Tom Coxeter, CITY=San Francisco, 94114, COUNTRY=US \|NAME=MONTSERRAT, Francesc, CITY=San Francisco, 94114, COUNTRY=US	(EP4166641)\|45	3	1					(EP4166641)\|Number of Claims: NCL=10\|Primary examiner: Cubas Alcaraz, Jose\|		(EP4166641)\|ENGLISH (ENG)	(EP4166641)\|Patent	Titre: (EP4166641)\|Systems and methods for processing olivine Résumé: (EP4166641)\|The present disclosure provides a system for processing olivine. The system may comprise a reactor for accelerating olivine weathering. The reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering.	35	Abstract	gpt-4o-mini	yes	The article describes a system for processing olivine to accelerate its weathering, which is directly related to enhanced weathering for CO₂ capture.
41	CN202510926442	US19/420,413\|CN202510926442	US20260104346\|CN120404566\|CN120404566	115489354	US20260104346 A1 2026-04-16 [US20260104346]\|CN120404566 B 2025-09-05 [CN120404566B]\|CN120404566 A 2025-08-01 [CN120404566]	2025-07-07	2025-12-15\|2025-07-07	2026-04-16\|2025-09-05\|2025-08-01	\|(CN120404566B)\|2025-09-05	(US20260104346)\|2045-12-15\|(CN120404566)\|2045-07-07	(US20260104346)\|An Experimental System for Rock Corrosion by Supercritical Carbon Dioxide	(US20260104346)\|The present invention relates to an experimental system and usage method for supercritical carbon dioxide rock corrosion. The experimental system comprises a corrosion vessel for exposing samples to a saturated carbon dioxide aqueous solution. The inside of the corrosion vessel is provided with a heating assembly and a rock sample placement rack. The top of the rock sample placement rack is above the liquid level of saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is submerged in saturated carbon dioxide aqueous solution. The heating assembly is located on the perimeter wall of the corrosion vessel and connected with a controller. The corrosion vessel is connected to a carbon dioxide gas delivery unit and a booster pump assembly connected via a conveying pipe. The present invention enables rocks to corrode in both supercritical and carbon dioxide solutions.	CHINA UNIVERSITY OF MINING & TECHNOLOGY\|SHAOXING UNIVERSITY	(US20260104346)\|Shaoxing University ([CN])\|China University of Mining and Technology ([CN])\|(CN120404566)\|CHINA UNIVERSITY OF MINING & TECHNOLOGY ([CN])\|(CN120404566)\|CHINA UNIVERSITY OF MINING & TECHNOLOGY ([CN])	YANG Shengqi\|LI Yue\|HUANG Yanhua\|YIN Pengfei\|TIAN Wenling\|ZHU Zhennan	(US20260104346)\|YANG Shengqi\|LI Yue\|HUANG Yanhua\|YIN Pengfei\|TIAN Wenling\|ZHU Zhennan	(CN120404566)\|JI LI;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP)\|Reg. Nb: 61223	(US20260104346)\|Accordingly it is of great significance to provide an experimental system to study the corrosion of rock in geological storage environments comprising supercritical carbon dioxide.\|	(US20260104346)\|1. An experimental system for assaying rock corrosion in supercritical carbon dioxide, comprising a corrosion vessel (1), wherein: the corrosion vessel (1) contains saturated carbon dioxide aqueous solution; a top opening of the corrosion vessel (1) is connected with a sealing cover; the corrosion vessel (1) is provided with a heating assembly and contains a rock sample placement rack; a top of the rock sample placement rack is located above the liquid level of the saturated carbon dioxide aqueous solution, and a bottom of the rock sample placement rack is submerged in the saturated carbon dioxide aqueous solution; the heating assembly is arranged on a perimeter wall of the corrosion vessel (1) and connected with a controller (6); the controller (6) regulates the temperature of the heating assembly, and is capable of regulating the temperature of the heating assembly to provide conditions for maintaining a carbon dioxide supercritical state; the corrosion vessel (1) is connected with a carbon dioxide gas conveying unit through a conveying pipe, and the carbon dioxide gas conveying unit comprises: a gas source storage tank (5) configured to supply carbon dioxide gas, wherein the gas source storage tank (5) has a gas outlet; a gas booster pump assembly, configured to provide conditions for maintaining a supercritical state of carbon dioxide, wherein the gas booster pump assembly and the gas outlet are connected through a pipeline, and the gas booster pump assembly is connected to the conveying pipe; the corrosion vessel (1) comprises two independent corrosion chambers, a first corrosion chamber and a second corrosion chamber, and the first corrosion chamber and the second corrosion chamber are both configured to contain saturated carbon dioxide aqueous solution; at least two rock sample placement racks are provided, and each rock sample placement rack is respectively provided in the first corrosion chamber and the second corrosion chamber; the sealing cover includes a first sealing cover (2) and a second sealing cover (101); the first sealing cover (2) is threadedly connected to the top opening of the first corrosion chamber, and the second sealing cover (101) is threadedly connected to the bottom opening of the second corrosion chamber; the delivery pipe includes a first transmission pipe and a second transmission pipe; the first transmission pipe and the second transmission pipe are both connected to the gas booster pump assembly through a pipeline; the first transmission pipe passes through the first sealing cover (2) and is connected to the first corrosion chamber, and the second transmission pipe is connected to the second corrosion chamber.\|	(US20260104346)\|As shown in FIGS. 1 to 8, the present invention provides an experimental system for supercritical carbon dioxide rock corrosion, including a corrosion vessel 1, wherein the corrosion vessel 1 is used to store a saturated carbon dioxide aqueous solution, and the top of the corrosion vessel 1 is open and connected to a sealing cover, and a heating component and a rock sample placement rack are provided inside the corrosion vessel 1, wherein the top of the rock sample placement rack is located above the liquid surface of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is immersed in the saturated carbon dioxide aqueous solution, and the heating component is provided on the peripheral wall of the corrosion vessel 1 and connected to a controller 6, wherein the controller 6 regulates the temperature of the heating component so that the temperature of the heating component after regulation provides a temperature that maintains the supercritical state of carbon dioxide.\|The present invention relates to an experimental system and usage method for supercritical carbon dioxide rock corrosion.\|To address the shortcomings of the prior art, the present invention aims to provide a supercritical CO_2 rock corrosion experimental system and method of use.\|	(US20260104346)\|SUPERCRITICAL CARBON DIOXIDE(100,29)\|EXPERIMENTAL SYSTEM(100,19)\|ASSAYING ROCK CORROSION(100,7)\|STONE CORROSION(100,2)\|CORROSION VESSEL(96,58)\|CORROSION CHAMBER(75,33)\|PLACEMENT RACK(71,16)\|ROCK SAMPLE PLACEMENT RACK(56,4)\|CARBON DIOXIDE SATURATION(48,20)\|TRANSMISSION PIPE(43,12)\|CONVEYING PIPE(42,8)\|AQUEOUS SOLUTION(40,20)\|GAS BOOSTER PUMP(35,32)\|CORROSION VESSEL PERIMETER WALL(34,3)\|ROCK CORROSION(34,1)\|SEALING(32,40)\|ROCK BOTTOM(26,4)\|PIPELINE(25,19)\|PERIMETER WALL(22,3)\|HEATING COMPONENT(21,7)\|CONVEYER PIPE(21,6)\|CORROSION VESSEL PERIPHERAL WALL(21,1)\|TEFLON CLAD WIRE(20,2)\|ROCK(19,18)\|CARBON DIOXIDE GAS(19,17)\|SIGNIFICANCE(19,1)\|DELIVERY PIPE(18,7)\|GAS OUTLET(18,7)\|HEATING TEMPERATURE(18,7)\|CORROSION CHAMBER THREAD(18,3)\|GEOLOGICAL STORAGE ENVIRONMENT(16,7)\|CORROSION VESSEL TOP(16,1)\|MAINTAINING CARBON DIOXIDE(16,1)\|REGULATION(16,1)\|CORROSION(14,10)\|PERIPHERAL WALL(14,1)\|SUPERCRITICAL PHASE(13,3)\|HEATING COMPONENT TEMPERATURE(12,3)\|ANTI CORROSION ALLOY(12,2)\|THREADED INTERFACE(11,2)\|CARBON DIOXIDE(10,17)\|GAS SOURCE STORAGE TANK(10,9)\|PRESSURIZING(10,3)\|CORROSION CHAMBER BOTTOM OPENING(10,2)\|BUFFER VESSEL AIR INLET(9,3)\|CORROSION VESSEL TOP OPENING(9,2)\|SEALING RING(8,16)\|TOP OPENING(8,4)\|ROCK CORROSION EXPERIMENTAL SYSTEM(8,3)\|CORROSION CHAMBER TOP OPENING(8,2)\|GEOLOGICAL EXPLORATION(8,2)\|UPPER SLEEVE(8,2)\|PRESSURIZED CARBON DIOXIDE GAS(7,4)\|BUFFER VESSEL AIR OUTLET(7,3)\|BOTTOM OPENING(7,2)\|ROCK CORROSION SIMULATION EXPERIMENT(7,1)\|GEOLOGICAL SEQUESTRATION ENVIRONMENT(6,1)\|SEALING COVER(5,5)\|ROCK COEXISTENCE(5,1)\|ROCK CORROSION CURING(5,1)\|SIMULTANEOUS CORROSION EXPERIMENT(5,1)\|INLET PIPE(4,7)\|CARBON DIOXIDE GROUNDWATER SOLUTION(4,3)\|LIQUID LEVEL(4,3)\|CORROSION RESISTANT ALLOY(4,2)\|ENTRY PIPE(4,2)\|PRESSURE GAUGE(3,10)\|GAS SOURCE TANK(3,6)\|DRIVE CYLINDER(3,5)\|LIQUID PHASE ENVIRONMENT(3,4)\|TEMPERATURE CONTROLLER(3,4)\|DELIVERY UNIT(3,3)\|OUTLET END(3,3)\|CORROSION PRODUCT(3,2)\|GAS SCREW INTERFACE(3,2)\|MINERAL(3,2)\|ROCK SAMPLE HOLDER(3,2)\|SPECIMEN(3,2)\|CORROSION ASSAY(3,1)\|EXPOSING ROCK(3,1)\|ORDINARY SKILL PERSON(3,1)\|POLYTETRAFLUOROETHYLENE(3,1)\|SEALING MIDDLE(3,1)\|VESSEL CORROSION(3,1)\|\|(CN120404566)\|CARBON DIOXIDE(100,103)\|CONVEYING PIPE(100,20)\|EXPERIMENTAL SYSTEM(100,17)\|CARBON DIOXIDE ROCK CORROSION(100,16)\|STONE CORROSION(100,16)\|CORROSION CHAMBER(88,40)\|CORROSION VESSEL(83,11)\|CORROSION CONTAINER(82,52)\|CORROSION VESSEL PERISPORIUM(72,1)\|GEOLOGICAL SEQUESTRATION ENVIRONMENT(60,1)\|ROCK CORROSION EXPERIMENT(56,3)\|GEOLOGICAL EXPLORATION(43,2)\|ROCK(40,17)\|ROCK SAMPLE PLACING RACK(40,5)\|ROCK BOTTOM SUBMERGENCE(39,1)\|PLACING RACK(38,4)\|CARBON DIOXIDE GROUNDWATER SOLUTION(38,3)\|GAS OUTLET(37,11)\|ROCK SAMPLE RACK(36,2)\|CONVEYER PIPE(35,2)\|GAS BOOSTER PUMP(34,29)\|SUPERCRITICAL CARBON DIOXIDE(34,9)\|EXPERIMENT(34,7)\|CARBONATE ROCK(34,1)\|PIPELINE(33,19)\|COEXISTENCE(32,2)\|SAMPLE PLACEMENT(31,5)\|SEALING(30,33)\|BUFFER CONTAINER(30,21)\|AQUEOUS SOLUTION(30,18)\|MINERAL(30,2)\|CONVEYING GAS(30,1)\|GROUNDWATER SOLUTION(28,1)\|GAS BOOSTER PUMP COMPONENT(27,2)\|BOTTOM SUBMERGENCE(27,1)\|PIPELINE EXTERIOR(27,1)\|RESISTANT CORROSION RESISTANT ALLOY(27,1)\|ROCK SAMPLE PLACING FRAME(26,6)\|CARBON DIOXIDE AQUEOUS SOLUTION(25,18)\|GAS SOURCE TANK(25,2)\|CARBON DIOXIDE GAS CONVEYING(24,1)\|CORROSION CHAMBER BOTTOM(24,1)\|INORGANIC PHASE(24,1)\|HEATING COMPONENT(22,11)\|SEALING COVER(22,8)\|CARBON DIOXIDE GAS(21,13)\|THREADED CONNECTION(21,11)\|CORROSION CONTAINER PERIPHERAL WALL(21,3)\|RACK(21,3)\|POLYTETRAFLUOROETHYLENE COATED WIRE(21,2)\|ROCK CHEMICAL PROPERTY(21,1)\|SEALING LID(20,7)\|GEOLOGICAL STORAGE ENVIRONMENT(20,5)\|ROCK BOTTOM(20,2)\|WATER SOLUTION(20,2)\|CORROSION CHAMBER TOP(20,1)\|CONVEYER(19,2)\|REGULATION(19,2)\|BUFFER VESSEL(19,1)\|SILICATE(18,1)\|CARBON DIOXIDE WATER SOLUTION(17,2)\|UPPER CORROSION CHAMBER(17,2)\|SUPERCRITICAL PHASE(16,4)\|HEATING ELEMENT(15,5)\|DELIVERY PIPE(15,3)\|PERIPHERAL WALL(14,3)\|SUPPLYING CARBON DIOXIDE(14,3)\|CHEMICAL PROPERTY(14,2)\|TRUE RESEARCH DATA(14,1)\|MUTUALLY INDEPENDENT(13,2)\|RESEARCH DATA RELIABILITY(13,1)\|CARBON DIOXIDE SOLUTION(12,5)\|BOOSTED CARBON DIOXIDE(12,3)\|THREADED INTERFACE(12,3)\|GAS INLET(12,1)\|BOOSTING(11,3)\|CORROSION CONTAINER TOP OPENING(11,2)\|SEALING RING(10,16)\|PIPE INTRODUCTION(9,6)\|CHEMICAL ENGINEERING(9,2)\|MATERIALS SCIENCE(9,1)\|ROCK CORROSION SIMULATION EXPERIMENT(9,1)\|HEATING COMPONENT TEMPERATURE(8,4)\|HEATING TEMPERATURE(7,4)\|CARBON DIOXIDE PRESSURE(7,1)\|TEMPERATURE RESISTANT PRESSURE(7,1)\|GAS SOURCE STORAGE TANK(6,9)\|DRIVING CYLINDER(6,5)\|TRANSMISSION PIPE(6,5)\|LIQUID LEVEL(6,4)\|TOP OPENING(6,3)\|ROCK CORROSION MAINTENANCE(6,1)\|AIR SOURCE STORAGE TANK(5,6)\|PRESSURIZED CARBON DIOXIDE(5,4)\|GEOLOGICAL SEALING ENVIRONMENT(5,1)\|MUTUAL INDEPENDENCE CORROSION CHAMBER(5,1)\|PRESSURE GAUGE(4,10)\|LIQUID PHASE ENVIRONMENT(4,4)\|TRANSFER PIPE(4,3)\|CORROSION RESEARCH(4,1)\|POLYTETRAFLUOROETHYLENE COVERED WIRE(4,1)\|SEALED LID CORROSION CHAMBER(4,1)\|\|(CN120404566)\|CARBON DIOXIDE(100,102)\|CORROSION CONTAINER(100,58)\|EXPERIMENTAL SYSTEM(100,17)\|CARBON DIOXIDE ROCK CORROSION(100,16)\|STONE CORROSION(100,16)\|ROCK CORROSION EXPERIMENT(63,4)\|CONVEYING PIPE(59,16)\|CORROSION CHAMBER(57,40)\|GEOLOGICAL SEQUESTRATION ENVIRONMENT(56,1)\|GEOLOGICAL EXPLORATION(40,2)\|ROCK SAMPLE PLACING RACK(37,5)\|SUPERCRITICAL CARBON DIOXIDE(36,10)\|PLACING RACK(36,4)\|CARBON DIOXIDE GROUNDWATER SOLUTION(36,3)\|GAS OUTLET(35,11)\|ROCK SAMPLE RACK(34,2)\|ROCK(33,16)\|CONVEYER PIPE(33,2)\|PIPELINE(32,20)\|EXPERIMENT(32,7)\|CARBONATE ROCK(32,1)\|GAS BOOSTER PUMP(30,29)\|COEXISTENCE(30,2)\|SAMPLE PLACEMENT(29,5)\|BUFFER CONTAINER(28,21)\|MINERAL(28,2)\|GROUNDWATER SOLUTION(27,1)\|PERISPORIUM(27,1)\|RESISTANT CORROSION RESISTANT ALLOY(26,1)\|GAS BOOSTER PUMP COMPONENT(25,2)\|GAS SOURCE TANK(24,2)\|INORGANIC PHASE(22,1)\|HEATING COMPONENT(21,11)\|CORROSION CONTAINER PERIPHERAL WALL(20,3)\|ROCK CHEMICAL PROPERTY(20,1)\|SEALING LID(19,7)\|GEOLOGICAL STORAGE ENVIRONMENT(19,5)\|ROCK BOTTOM(19,2)\|WATER SOLUTION(19,2)\|AQUEOUS SOLUTION(18,16)\|REGULATION(18,2)\|BUFFER VESSEL(18,1)\|CORROSION VESSEL(17,5)\|SILICATE(17,1)\|CARBON DIOXIDE GAS(16,12)\|CARBON DIOXIDE WATER SOLUTION(16,2)\|CARBON DIOXIDE AQUEOUS SOLUTION(15,16)\|THREADED CONNECTION(15,11)\|SUPERCRITICAL PHASE(15,4)\|SEALING COVER(14,7)\|HEATING ELEMENT(14,5)\|ROCK SAMPLE PLACING FRAME(14,5)\|DELIVERY PIPE(14,3)\|PERIPHERAL WALL(14,3)\|GAS DELIVERY UNIT(14,2)\|SUPPLYING CARBON DIOXIDE(13,3)\|CHEMICAL PROPERTY(13,2)\|RESEARCH DATA RELIABILITY(13,1)\|TRUE RESEARCH DATA(13,1)\|CARBON DIOXIDE SOLUTION(12,5)\|BOOSTED CARBON DIOXIDE(12,3)\|THREADED INTERFACE(12,3)\|GAS INLET(12,1)\|BOOSTING(10,3)\|CORROSION CONTAINER TOP OPENING(10,2)\|SEALING RING(9,16)\|UPPER CORROSION CHAMBER(9,2)\|PIPE INTRODUCTION(8,6)\|HEATING COMPONENT TEMPERATURE(8,4)\|TOP OPENING(8,4)\|CHEMICAL ENGINEERING(8,2)\|MATERIALS SCIENCE(8,1)\|ROCK CORROSION SIMULATION EXPERIMENT(8,1)\|HEATING TEMPERATURE(7,4)\|CORROSION CHAMBER BOTTOM OPENING(7,2)\|CARBON DIOXIDE PRESSURE(6,1)\|ROCK CORROSION MAINTENANCE(6,1)\|TEMPERATURE RESISTANT PRESSURE(6,1)\|GAS SOURCE STORAGE TANK(5,9)\|DRIVING CYLINDER(5,5)\|TRANSMISSION PIPE(5,5)\|PRESSURIZED CARBON DIOXIDE(5,4)\|CORROSION CHAMBER TOP OPENING(5,2)\|GEOLOGICAL SEALING ENVIRONMENT(5,1)\|MUTUAL INDEPENDENCE CORROSION CHAMBER(5,1)\|PRESSURE GAUGE(4,10)\|AIR SOURCE STORAGE TANK(4,6)\|LIQUID PHASE ENVIRONMENT(4,4)\|TRANSFER PIPE(4,3)\|CORROSION RESEARCH(4,1)\|POLYTETRAFLUOROETHYLENE COATED WIRE(4,1)\|POLYTETRAFLUOROETHYLENE COVERED WIRE(4,1)\|SEALED LID CORROSION CHAMBER(4,1)\|TEMPERATURE CONTROLLER(3,5)\|DEFECT(3,2)\|	(US20260104346)\|What is claimed is:\|1. An experimental system for assaying rock corrosion in supercritical carbon dioxide, comprising a corrosion vessel (1), wherein:\| the corrosion vessel (1) contains saturated carbon dioxide aqueous solution;\| a top opening of the corrosion vessel (1) is connected with a sealing cover;\| the corrosion vessel (1) is provided with a heating assembly and contains a rock sample placement rack;\| a top of the rock sample placement rack is located above the liquid level of the saturated carbon dioxide aqueous solution, and a bottom of the rock sample placement rack is submerged in the saturated carbon dioxide aqueous solution;\| the heating assembly is arranged on a perimeter wall of the corrosion vessel (1) and connected with a controller (6);\| the controller (6) regulates the temperature of the heating assembly, and is capable of regulating the temperature of the heating assembly to provide conditions for maintaining a carbon dioxide supercritical state;\| the corrosion vessel (1) is connected with a carbon dioxide gas conveying unit through a conveying pipe, and the carbon dioxide gas conveying unit comprises:\| a gas source storage tank (5) configured to supply carbon dioxide gas, wherein the gas source storage tank (5) has a gas outlet;\| a gas booster pump assembly, configured to provide conditions for maintaining a supercritical state of carbon dioxide, wherein the gas booster pump assembly and the gas outlet are connected through a pipeline, and the gas booster pump assembly is connected to the conveying pipe;\| the corrosion vessel (1) comprises two independent corrosion chambers, a first corrosion chamber and a second corrosion chamber, and the first corrosion chamber and the second corrosion chamber are both configured to contain saturated carbon dioxide aqueous solution;\| at least two rock sample placement racks are provided, and each rock sample placement rack is respectively provided in the first corrosion chamber and the second corrosion chamber;\| the sealing cover includes a first sealing cover (2) and a second sealing cover (101);\| the first sealing cover (2) is threadedly connected to the top opening of the first corrosion chamber, and the second sealing cover (101) is threadedly connected to the bottom opening of the second corrosion chamber;\| the delivery pipe includes a first transmission pipe and a second transmission pipe;\| the first transmission pipe and the second transmission pipe are both connected to the gas booster pump assembly through a pipeline;\| the first transmission pipe passes through the first sealing cover (2) and is connected to the first corrosion chamber, and the second transmission pipe is connected to the second corrosion chamber.\|2. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, wherein the gas booster pump assembly comprises a gas booster pump (4) and a buffer vessel (3);\| wherein the buffer vessel (3) is arranged between the gas booster pump (4) and the corrosion vessel (1), and the air inlet of the buffer vessel (3) is connected to the gas booster pump (4) through a pipeline, and the air outlet of the buffer vessel (3) is connected to the corrosion vessel (1) through a conveying pipe.\|3. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 2, wherein the corrosion vessel (1) and the buffer vessel (3) are both made of high-temperature and pressure-resistant anti-corrosion alloy.\|4. The experimental system for rock corrosion in supercritical carbon dioxide according to claim 1, wherein a pressure gauge and a needle pressure control valve configured to regulate carbon dioxide pressure levels are provided on the conveyor pipe.\|5. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, wherein the first sealing cover (2) has a first sealing body (201) threaded with the first corrosion chamber, the second sealing cover (101) has a second sealing body connected with the second corrosion chamber thread, and the first sealing body (201) and the second sealing body are provided with a first sealing ring (202) and a second sealing ring (203) on the upper and lower sleeves.\|6. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, wherein the distance between the first sealing ring (202) and the second sealing ring (203) is 5cm˜5.2cm.\|7. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, wherein all pipelines are provided with threaded interfaces at the inlet and outlet ends, and all pipelines are equipped with teflon clad wires on the outside.\|8. A method of using the experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, comprising the following steps:\| a rock sample is placed on the rock sample placement rack, and the saturated carbon dioxide aqueous solution is filled into the corrosion vessel (1), so that the lower part of the rock sample is immersed in the saturated carbon dioxide aqueous solution;\| the gas source storage tank (5) is opened, sending the carbon dioxide in the gas source storage tank (5) into the gas booster pump (4) for pressurization, and the pressurized carbon dioxide is sent into the corrosion vessel (1) through the conveyor pipe;\| the heating temperature of the heating assembly is adjusted by the controller to convert the pressurized carbon dioxide gas fed into the corrosion vessel (1) into supercritical carbon dioxide, so that the rock samples on the rock sample placement rack are placed in the supercritical phase and liquid phase environment.	(US20260104346)\|TECHNICAL FIELD\|[0001] The present invention relates to the field of rock corrosion experimental technology, and more specifically, to an experimental system and method for testing the effects of supercritical carbon dioxide on rock corrosion.\|BACKGROUND\|[0002] Supercritical carbon dioxide rock corrosion assays are used to study the physical and chemical properties of petrochemicals, mainly by testing the changes in chemical composition in rocks to analyze the strength performance of specimens. This type of experiment has a wide range of applications in materials science, chemical engineering, and geological exploration.\|[0003] In a carbon dioxide geological sequestration environment, a rock/supercritical carbon dioxide/carbon dioxide groundwater solution exists in phase equilibrium. Supercritical carbon dioxide can dissolve certain minerals in rock, including carbonate rock, which may lead to changes in the physical and chemical properties of the rock. The carbon-dioxide groundwater solution will react with certain minerals in rock (such as silicates) and may form new mineral phases, which may have different physical and chemical properties, thus affecting the properties of the rock, Thus, it is necessary to study petrology while supercritical carbon dioxide-carbon dioxide groundwater solutions are in coexistence to provide empirical, reliable research data for materials science, chemical engineering and geological exploration. However, there are no device in existence that can provide a suitable environment for exposing rock samples to corrosion in supercritical phase and liquid phase environments at the same temperature and pressure. Accordingly it is of great significance to provide an experimental system to study the corrosion of rock in geological storage environments comprising supercritical carbon dioxide.\|SUMMARY\|[0004] In view of the shortcomings of the above prior art, the purpose of the present invention is to provide an experimental system and usage method for supercritical carbon dioxide rock corrosion, which can corrode rocks in supercritical carbon dioxide and carbon dioxide solution at the same temperature and pressure state of a carbon dioxide geological storage environment.\|[0005] In order to solve the above technical problems, the present invention adopts the following technical scheme:\|[0006] The present invention provides an experimental system for supercritical carbon dioxide rock corrosion, comprising a corrosion vessel, wherein the corrosion vessel is used to store a saturated carbon dioxide aqueous solution. A top opening of the corrosion vessel is connected with a sealing cover, and the inside of the corrosion vessel is provided with a heating assembly and a rock sample placement rack. The top of the rock sample placement rack is located above the liquid level of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is submerged in the saturated carbon dioxide aqueous solution. The heating assembly is arranged on the perimeter wall of the corrosion vessel and is connected with a controller. The controller regulates the temperature of the heating assembly, and is used to make the temperature of the heating assembly suitable for maintaining a supercritical state of carbon dioxide.\|[0007] The corrosion vessel is connected with a carbon dioxide gas conveying unit through a conveying pipe, and the carbon dioxide gas conveying unit comprises:\|[0008] A gas source storage tank, used to supply carbon dioxide gas, wherein the gas source storage tank has a gas outlet;\|[0009] A gas booster pump assembly, used to provide conditions for maintaining a supercritical state of carbon dioxide, wherein the gas booster pump assembly and gas outlet are connected through pipelines, and the gas booster pump assembly is connected to the conveying pipe.\|[0010] Preferably, the gas booster pump assembly comprises a gas booster pump and a buffer vessel, with the buffer vessel arranged between the gas booster pump and the corrosion vessel, and the air inlet of the buffer vessel connected to the gas booster pump through a pipeline. The air outlet of the buffer vessel is connected to the corrosion vessel through a conveying pipe.\|[0011] Preferably, the corrosion vessel and the buffer vessel are made of high-temperature and pressure-resistant anti-corrosion alloy.\|[0012] Preferably, the conveyor pipe is provided with a pressure gauge and a needle pressure control valve for regulating the amount of carbon dioxide pressure.\|[0013] Preferably, the corrosion vessel comprises a first corrosion chamber and a second corrosion chamber. Saturated carbon dioxide aqueous solution is stored in the first corrosion chamber and the second corrosion chamber, and the rock sample placement rack is set in each corrosion chamber. Each rock sample placement rack is arranged in the first corrosion chamber and the second corrosion chamber respectively, and the sealing cover comprises the first sealing cover and the second sealing cover. The first sealing cover is connected with the top open thread of the first corrosion chamber, the second sealing cover is connected with the bottom open thread of the second corrosion chamber via a transmission pipe and a conveyor pipe. The transmission pipe and the conveyor pipe are connected with the gas booster pump assembly through a pipeline, wherein the transmission pipe runs through the first sealing cover and is connected to the first corrosion chamber, and the transfer pipe is connected with the second corrosion chamber.\|[0014] Preferably, the first sealing cover has a first sealing body connected with the first corrosion chamber thread, and the second sealing cover has a second sealing body connected with the second corrosion chamber thread, and the first sealing body and the second sealing body are provided with a first sealing ring and a second sealing ring on the upper and lower sleeves.\|[0015] Preferably, the distance between the first sealing ring and the second sealing ring is 5cm˜5.2cm.\|[0016] Preferably, all pipelines are provided with threaded interfaces at the inlet and outlet ends, and all pipelines are equipped with Teflon clad wires on the outside.\|[0017] The present invention also gives a method for the use of an experimental system for supercritical carbon dioxide rock corrosion, comprising the following steps:\|[0018] The rock sample is placed on the rock sample placement rack, and the corrosion vessel is filled with saturated carbon dioxide aqueous solution, so that the lower part of the rock sample is immersed in the saturated carbon dioxide aqueous solution.\|[0019] Then the gas source storage tank is opened, and the carbon dioxide in the gas source storage tank is sent to the gas booster pump for pressurization. The pressurized carbon dioxide is sent into the corrosion vessel through the conveyor pipe.\|[0020] The heating temperature of the heating component is controlled by the controller to convert the pressurized carbon dioxide gas sent into the corrosion vessel into supercritical carbon dioxide, so that the rock samples on the rock sample placement rack are placed in the supercritical phase and liquid phase environment.\|[0021] The beneficial effects of the present invention compared with the prior art:\|[0022] The experimental system for supercritical carbon dioxide rock corrosion given by the present invention can perform rock corrosion simulation experiments for the carbon dioxide geological storage environment, and solve the disadvantages that the existing devices cannot simulate the carbon dioxide geological storage environment for rock corrosion simulation experiments under the same temperature and pressure state.\|[0023] During experiments, the carbon dioxide gas is pressurized by the gas booster pump assembly and sent into the corrosion vessel through the conveying pipe. In order to make the carbon dioxide feed into the corrosion vessel at a pressure of 7.38 MPa to reach the supercritical state, the temperature of the heating component is controlled by the controller, and the pressurized carbon dioxide sent into the corrosion vessel can reach the temperature of 31.1° C. in the corrosive vessel. Under these conditions when carbon dioxide reaches the supercritical state, the corrosion vessel realizes the simulation of the carbon dioxide geological storage environment. This system overcomes the shortcoming that devices in the existing technology cannot corrode the rock in the liquid phase and the supercritical carbon dioxide gas phase at the same time.\|[0024] The buffer vessel is provided in the present invention not only for sending the high-pressure carbon dioxide gas boosted by the gas booster pump into the buffer vessel for storage, but also for ensuring that the pressurized carbon dioxide gas can be sent into the corrosion vessel at a stable pressure.\|(US20260104346)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0025] FIG. 1 is a schematic diagram of the overall structure of a supercritical carbon dioxide rock corrosion curing test device proposed by the present invention in a high temperature and high pressure environment.\|[0026] FIG. 2 shows the structure of the corrosion vessel.\|[0027] FIG. 3 is a schematic diagram of the structure of the high-pressure sealing cover.\|[0028] FIG. 4 shows the structure of the buffer vessel.\|[0029] FIG. 5 shows the schematic diagram of the gas booster pump structure (front).\|[0030] FIG. 6 shows the schematic diagram of the gas booster pump structure (back).\|[0031] FIG. 7 shows the schematic diagram of the carbon dioxide gas source structure.\|[0032] FIG. 8 shows the structure of the controller, temperature controller, and resistive heating plate.\|(US20260104346)\|REFERENCE NUMERALS\|[0033] 1. Corrosion vessel; 101. a second sealing cover; 102. a first pressure gauge; 103. a first needle pressure regulator; 2. the first sealing cover; 201. The first seal; 202. a first sealing ring; 203. a second sealing ring; 204. a second-needle pressure regulator; 205. a second pressure gauge; 206. The first inlet pipe; 207. High-pressure gas screw interface; 3. Buffer vessel; 301. a pressure buffer tank; 302. the first high-voltage interface screw; 303. a high-pressure gas three-way valve; 304. a second high-voltage interface screw; 305. a second entry pipe; 4. a gas booster pump; 401. a supercharged cylinder block; 402. a drive cylinder; 403. a low air pressure air inlet; 404. a third entry pipe; 405. a high-pressure air outlet; 5. an air source storage tank; 501. a gas pressure reducing valve; 502. an air source switch ball valve; 503. a high-concentration carbon dioxide cylinder; 6. Controller, 601, temperature controller, 602, resistance heating plate.\|DETAILED DESCRIPTION OF EMBODIMENTS\|[0034] The following describes in detail the specific embodiments of the present invention, but it should be understood that the scope of protection of the present invention is not limited by the specific embodiments. Based on the embodiments of the present invention, all other embodiments obtained by persons of ordinary skill in the art without inventive effort are within the scope of protection of the present invention. The experimental methods described in the embodiments of the present invention are conventional methods unless otherwise specified. The inventors have discovered that existing rock corrosion experimental systems all conduct corrosion studies by immersing granite in a high-pressure reactor filled with supercritical carbon dioxide. The experimental device of the present invention primarily considers the coexistence of rock and supercritical CO2—CO2 groundwater solution in a CO2 geological storage environment. Simultaneous corrosion experiments on rock in both environments are more realistic. To address the shortcomings of the prior art, the present invention aims to provide a supercritical CO2 rock corrosion experimental system and method of use. This experimental system can simultaneously corrode rock in both a supercritical state and a CO2 solution in a CO2 geological storage environment. As shown in FIGS. 1 to 8, the present invention provides an experimental system for supercritical carbon dioxide rock corrosion, including a corrosion vessel 1, wherein the corrosion vessel 1 is used to store a saturated carbon dioxide aqueous solution, and the top of the corrosion vessel 1 is open and connected to a sealing cover, and a heating component and a rock sample placement rack are provided inside the corrosion vessel 1, wherein the top of the rock sample placement rack is located above the liquid surface of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is immersed in the saturated carbon dioxide aqueous solution, and the heating component is provided on the peripheral wall of the corrosion vessel 1 and connected to a controller 6, wherein the controller 6 regulates the temperature of the heating component so that the temperature of the heating component after regulation provides a temperature that maintains the supercritical state of carbon dioxide. Conditions are established to ensure that the carbon dioxide delivered into the corrosion vessel 1 reaches a supercritical temperature of 31.1° C. The corrosion vessel 1 is connected to a carbon dioxide gas delivery unit via a delivery pipe. The carbon dioxide gas delivery unit comprises:\|[0035] A gas source tank 5 for supplying carbon dioxide gas and having a gas outlet. The gas source tank 5 comprises a high-concentration carbon dioxide cylinder 503, a gas pressure reducing valve 501, and a gas source on/off ball valve 502. A pipeline is connected to the top of the high-concentration carbon dioxide cylinder 503. The pipeline near the outlet is equipped with a gas source on/off ball valve 502 and a gas pressure reducing valve 501. The gas outlet of the gas source tank 5 is the outlet of the pipeline to which the gas source tank 5 is connected. A gas booster pump assembly is connected to the gas outlet (pipeline output) via a pipeline. The gas booster pump assembly is connected to the delivery pipe. The gas booster pump assembly ensures that the carbon dioxide delivered into the corrosion vessel 1 reaches a supercritical pressure of 7.38 MPa. The gas booster pump assembly includes a gas booster pump 4, which comprises a booster cylinder 401 and a drive cylinder 402. One end of the booster cylinder 401 is connected to the drive cylinder 402. One end of the drive cylinder 402 is provided with a low-pressure air inlet 403, which is connected to the gas source storage tank 5 via a third inlet pipe 404. The drive cylinder 402 is provided with a high-pressure air outlet 405, which is connected to the delivery pipe via a second inlet pipe 305. Specifically, the gas booster pump assembly includes the gas booster pump 4 and a buffer vessel 3. The buffer vessel 3 is located between the gas booster pump 4 and the corrosion vessel 1. The air inlet of the buffer vessel 3 is connected to the gas booster pump 4 via a pipeline, and the air outlet of the buffer vessel 3 is connected to the corrosion vessel 1 via a delivery pipe. Buffer vessel 3 comprises a pressure buffer tank 301, a first high-pressure interface screw 302, a high-pressure gas three-way valve 303, a second high-pressure interface screw 304, and a second inlet pipe 305. The top outlet of the pressure buffer tank 301 is connected to a pipeline via the first high-pressure interface screw 302, which is connected to one outlet of the high-pressure gas three-way valve 303. The second high-pressure interface screw 304 is located at one inlet of the high-pressure gas three-way valve 303 and is threadedly connected to the second inlet pipe 305. The other outlet of the high-pressure gas three-way valve 303 is connected to the corrosion vessel 1 via a delivery pipe. Specifically, both the corrosion vessel 1 and the buffer vessel 3 are made of a high-temperature, pressure-resistant, and corrosion-resistant alloy. This ensures that the materials of the buffer vessel 3 and the corrosion vessel 1 themselves are not corroded by CO2 during long-term corrosion testing, which would otherwise contaminate the specimens with corrosion products. Both the buffer vessel 3 and the corrosion vessel 1 are made of a high-temperature, corrosion-resistant alloy, alloy numbered GH4161. Specifically, the delivery pipe is equipped with a pressure gauge and a needle-type pressure control valve for adjusting the CO2 pressure. The pressure gauge includes a first pressure gauge 102 and a second pressure gauge 205, and the needle pressure control valve includes a first needle pressure regulating valve 103 and a second needle pressure regulating valve 204. This is intended to ensure that the buffer vessel 3 and corrosion vessel 1 materials themselves are not corroded by CO2 during long-term corrosion testing, which would otherwise cause corrosion products from the metal materials to contaminate the specimen. Both the buffer vessel 3 and corrosion vessel 1 are made of a high-temperature corrosion-resistant alloy, alloy number GH4161. Specifically, the corrosion vessel 1 comprises two independent upper and lower first and second corrosion chambers, each containing a saturated carbon dioxide solution. At least two rock sample racks are provided, one in each of the first and second corrosion chambers. The sealing covers comprise a first sealing cover 2 and a second sealing cover 101. The first sealing cover 2 is threadedly connected to the top opening of the first corrosion chamber, while the second sealing cover 101 is threadedly connected to the bottom opening of the second corrosion chamber. The delivery pipe comprises a transmission pipe and a transmission pipe, both of which are connected to the gas booster pump assembly via pipelines. The transmission pipe is connected to the high-pressure gas screw interface 207 at the end of the first inlet pipe 206, passes through the first sealing cover 2, and connects to the first corrosion chamber. The transmission pipe is connected to the second corrosion chamber. The first inlet pipe 206 is also connected to a second needle pressure regulating valve 204 and a second pressure gauge 205, while the transmission pipe is also connected to the first needle pressure regulating valve 103 and a first pressure gauge 102. Specifically, the first sealing cover 2 has a first sealing body 201 threadedly connected to the first corrosion chamber, and the second sealing cover 101 has a second sealing body threadedly connected to the second corrosion chamber. A first sealing ring 202 and a second sealing ring 203 are sleeved above and below the first sealing body 201 and the second sealing body. Specifically, the distance between the first sealing ring 202 and the second sealing ring 203 is 5 cm to 5.2 cm. The first sealing ring 202 is positioned in the middle of the first sealing body 201 or the second sealing body, and the second sealing ring 203 is positioned at the threaded end of the first sealing body 201 or the second sealing body, to provide a tighter connection between the first sealing cover 2 and the first corrosion chamber, or between the second sealing cover 101 and the second corrosion chamber. Specifically, all pipelines have threaded connections at the inlet and outlet ends, and all pipelines are covered with polytetrafluoroethylene (PTFE) wire. The threads at the pipeline connections ensure connection and replacement if damaged. The PTFE wire protects the pipelines from CO2 corrosion and is also wear-resistant. The present invention provides a method for using a supercritical carbon dioxide rock corrosion experimental system, comprising the following steps: Place a rock sample on a rock sample holder, and fill a corrosion vessel 1 with a saturated carbon dioxide aqueous solution so that the lower portion of the rock sample is immersed in the saturated carbon dioxide aqueous solution; Then, open a gas source tank 5, and pump the carbon dioxide in the gas source tank 5 into a gas booster pump 4 for pressurization. The pressurized carbon dioxide is then delivered to the corrosion vessel 1 through a delivery pipe. A controller 6 controls the heating temperature of a heating component to convert the pressurized carbon dioxide gas delivered to the corrosion vessel 1 into supercritical carbon dioxide, thereby placing the rock sample on the rock sample holder in a supercritical and liquid phase environment. Controller 6 includes a temperature controller 601 connected to a resistance heating element 602 for providing a constant temperature heat source for the corrosion vessel 1. The heating element is a resistance heating element 602. The desired temperature is set by the temperature controller 601, and the resistance heating element 602 provides a stable temperature. It is apparent that those skilled in the art may make various modifications and variations to the present invention without departing from the spirit and scope of the present invention. Thus, if these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is intended to include these modifications and variations.	(US20260104346)\|TECHNICAL FIELD\|[0001] The present invention relates to the field of rock corrosion experimental technology, and more specifically, to an experimental system and method for testing the effects of supercritical carbon dioxide on rock corrosion.\|BACKGROUND\|[0002] Supercritical carbon dioxide rock corrosion assays are used to study the physical and chemical properties of petrochemicals, mainly by testing the changes in chemical composition in rocks to analyze the strength performance of specimens. This type of experiment has a wide range of applications in materials science, chemical engineering, and geological exploration.\|[0003] In a carbon dioxide geological sequestration environment, a rock/supercritical carbon dioxide/carbon dioxide groundwater solution exists in phase equilibrium. Supercritical carbon dioxide can dissolve certain minerals in rock, including carbonate rock, which may lead to changes in the physical and chemical properties of the rock. The carbon-dioxide groundwater solution will react with certain minerals in rock (such as silicates) and may form new mineral phases, which may have different physical and chemical properties, thus affecting the properties of the rock, Thus, it is necessary to study petrology while supercritical carbon dioxide-carbon dioxide groundwater solutions are in coexistence to provide empirical, reliable research data for materials science, chemical engineering and geological exploration. However, there are no device in existence that can provide a suitable environment for exposing rock samples to corrosion in supercritical phase and liquid phase environments at the same temperature and pressure. Accordingly it is of great significance to provide an experimental system to study the corrosion of rock in geological storage environments comprising supercritical carbon dioxide.\|SUMMARY\|[0004] In view of the shortcomings of the above prior art, the purpose of the present invention is to provide an experimental system and usage method for supercritical carbon dioxide rock corrosion, which can corrode rocks in supercritical carbon dioxide and carbon dioxide solution at the same temperature and pressure state of a carbon dioxide geological storage environment.\|[0005] In order to solve the above technical problems, the present invention adopts the following technical scheme:\|[0006] The present invention provides an experimental system for supercritical carbon dioxide rock corrosion, comprising a corrosion vessel, wherein the corrosion vessel is used to store a saturated carbon dioxide aqueous solution. A top opening of the corrosion vessel is connected with a sealing cover, and the inside of the corrosion vessel is provided with a heating assembly and a rock sample placement rack. The top of the rock sample placement rack is located above the liquid level of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is submerged in the saturated carbon dioxide aqueous solution. The heating assembly is arranged on the perimeter wall of the corrosion vessel and is connected with a controller. The controller regulates the temperature of the heating assembly, and is used to make the temperature of the heating assembly suitable for maintaining a supercritical state of carbon dioxide.\|[0007] The corrosion vessel is connected with a carbon dioxide gas conveying unit through a conveying pipe, and the carbon dioxide gas conveying unit comprises:\|[0008] A gas source storage tank, used to supply carbon dioxide gas, wherein the gas source storage tank has a gas outlet;\|[0009] A gas booster pump assembly, used to provide conditions for maintaining a supercritical state of carbon dioxide, wherein the gas booster pump assembly and gas outlet are connected through pipelines, and the gas booster pump assembly is connected to the conveying pipe.\|[0010] Preferably, the gas booster pump assembly comprises a gas booster pump and a buffer vessel, with the buffer vessel arranged between the gas booster pump and the corrosion vessel, and the air inlet of the buffer vessel connected to the gas booster pump through a pipeline. The air outlet of the buffer vessel is connected to the corrosion vessel through a conveying pipe.\|[0011] Preferably, the corrosion vessel and the buffer vessel are made of high-temperature and pressure-resistant anti-corrosion alloy.\|[0012] Preferably, the conveyor pipe is provided with a pressure gauge and a needle pressure control valve for regulating the amount of carbon dioxide pressure.\|[0013] Preferably, the corrosion vessel comprises a first corrosion chamber and a second corrosion chamber. Saturated carbon dioxide aqueous solution is stored in the first corrosion chamber and the second corrosion chamber, and the rock sample placement rack is set in each corrosion chamber. Each rock sample placement rack is arranged in the first corrosion chamber and the second corrosion chamber respectively, and the sealing cover comprises the first sealing cover and the second sealing cover. The first sealing cover is connected with the top open thread of the first corrosion chamber, the second sealing cover is connected with the bottom open thread of the second corrosion chamber via a transmission pipe and a conveyor pipe. The transmission pipe and the conveyor pipe are connected with the gas booster pump assembly through a pipeline, wherein the transmission pipe runs through the first sealing cover and is connected to the first corrosion chamber, and the transfer pipe is connected with the second corrosion chamber.\|[0014] Preferably, the first sealing cover has a first sealing body connected with the first corrosion chamber thread, and the second sealing cover has a second sealing body connected with the second corrosion chamber thread, and the first sealing body and the second sealing body are provided with a first sealing ring and a second sealing ring on the upper and lower sleeves.\|[0015] Preferably, the distance between the first sealing ring and the second sealing ring is 5cm˜5.2cm.\|[0016] Preferably, all pipelines are provided with threaded interfaces at the inlet and outlet ends, and all pipelines are equipped with Teflon clad wires on the outside.\|[0017] The present invention also gives a method for the use of an experimental system for supercritical carbon dioxide rock corrosion, comprising the following steps:\|[0018] The rock sample is placed on the rock sample placement rack, and the corrosion vessel is filled with saturated carbon dioxide aqueous solution, so that the lower part of the rock sample is immersed in the saturated carbon dioxide aqueous solution.\|[0019] Then the gas source storage tank is opened, and the carbon dioxide in the gas source storage tank is sent to the gas booster pump for pressurization. The pressurized carbon dioxide is sent into the corrosion vessel through the conveyor pipe.\|[0020] The heating temperature of the heating component is controlled by the controller to convert the pressurized carbon dioxide gas sent into the corrosion vessel into supercritical carbon dioxide, so that the rock samples on the rock sample placement rack are placed in the supercritical phase and liquid phase environment.\|[0021] The beneficial effects of the present invention compared with the prior art:\|[0022] The experimental system for supercritical carbon dioxide rock corrosion given by the present invention can perform rock corrosion simulation experiments for the carbon dioxide geological storage environment, and solve the disadvantages that the existing devices cannot simulate the carbon dioxide geological storage environment for rock corrosion simulation experiments under the same temperature and pressure state.\|[0023] During experiments, the carbon dioxide gas is pressurized by the gas booster pump assembly and sent into the corrosion vessel through the conveying pipe. In order to make the carbon dioxide feed into the corrosion vessel at a pressure of 7.38 MPa to reach the supercritical state, the temperature of the heating component is controlled by the controller, and the pressurized carbon dioxide sent into the corrosion vessel can reach the temperature of 31.1° C. in the corrosive vessel. Under these conditions when carbon dioxide reaches the supercritical state, the corrosion vessel realizes the simulation of the carbon dioxide geological storage environment. This system overcomes the shortcoming that devices in the existing technology cannot corrode the rock in the liquid phase and the supercritical carbon dioxide gas phase at the same time.\|[0024] The buffer vessel is provided in the present invention not only for sending the high-pressure carbon dioxide gas boosted by the gas booster pump into the buffer vessel for storage, but also for ensuring that the pressurized carbon dioxide gas can be sent into the corrosion vessel at a stable pressure.\|(US20260104346)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0025] FIG. 1 is a schematic diagram of the overall structure of a supercritical carbon dioxide rock corrosion curing test device proposed by the present invention in a high temperature and high pressure environment.\|[0026] FIG. 2 shows the structure of the corrosion vessel.\|[0027] FIG. 3 is a schematic diagram of the structure of the high-pressure sealing cover.\|[0028] FIG. 4 shows the structure of the buffer vessel.\|[0029] FIG. 5 shows the schematic diagram of the gas booster pump structure (front).\|[0030] FIG. 6 shows the schematic diagram of the gas booster pump structure (back).\|[0031] FIG. 7 shows the schematic diagram of the carbon dioxide gas source structure.\|[0032] FIG. 8 shows the structure of the controller, temperature controller, and resistive heating plate.\|(US20260104346)\|REFERENCE NUMERALS\|[0033] 1. Corrosion vessel; 101. a second sealing cover; 102. a first pressure gauge; 103. a first needle pressure regulator; 2. the first sealing cover; 201. The first seal; 202. a first sealing ring; 203. a second sealing ring; 204. a second-needle pressure regulator; 205. a second pressure gauge; 206. The first inlet pipe; 207. High-pressure gas screw interface; 3. Buffer vessel; 301. a pressure buffer tank; 302. the first high-voltage interface screw; 303. a high-pressure gas three-way valve; 304. a second high-voltage interface screw; 305. a second entry pipe; 4. a gas booster pump; 401. a supercharged cylinder block; 402. a drive cylinder; 403. a low air pressure air inlet; 404. a third entry pipe; 405. a high-pressure air outlet; 5. an air source storage tank; 501. a gas pressure reducing valve; 502. an air source switch ball valve; 503. a high-concentration carbon dioxide cylinder; 6. Controller, 601, temperature controller, 602, resistance heating plate.\|DETAILED DESCRIPTION OF EMBODIMENTS\|[0034] The following describes in detail the specific embodiments of the present invention, but it should be understood that the scope of protection of the present invention is not limited by the specific embodiments. Based on the embodiments of the present invention, all other embodiments obtained by persons of ordinary skill in the art without inventive effort are within the scope of protection of the present invention. The experimental methods described in the embodiments of the present invention are conventional methods unless otherwise specified. The inventors have discovered that existing rock corrosion experimental systems all conduct corrosion studies by immersing granite in a high-pressure reactor filled with supercritical carbon dioxide. The experimental device of the present invention primarily considers the coexistence of rock and supercritical CO2—CO2 groundwater solution in a CO2 geological storage environment. Simultaneous corrosion experiments on rock in both environments are more realistic. To address the shortcomings of the prior art, the present invention aims to provide a supercritical CO2 rock corrosion experimental system and method of use. This experimental system can simultaneously corrode rock in both a supercritical state and a CO2 solution in a CO2 geological storage environment. As shown in FIGS. 1 to 8, the present invention provides an experimental system for supercritical carbon dioxide rock corrosion, including a corrosion vessel 1, wherein the corrosion vessel 1 is used to store a saturated carbon dioxide aqueous solution, and the top of the corrosion vessel 1 is open and connected to a sealing cover, and a heating component and a rock sample placement rack are provided inside the corrosion vessel 1, wherein the top of the rock sample placement rack is located above the liquid surface of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is immersed in the saturated carbon dioxide aqueous solution, and the heating component is provided on the peripheral wall of the corrosion vessel 1 and connected to a controller 6, wherein the controller 6 regulates the temperature of the heating component so that the temperature of the heating component after regulation provides a temperature that maintains the supercritical state of carbon dioxide. Conditions are established to ensure that the carbon dioxide delivered into the corrosion vessel 1 reaches a supercritical temperature of 31.1° C. The corrosion vessel 1 is connected to a carbon dioxide gas delivery unit via a delivery pipe. The carbon dioxide gas delivery unit comprises:\|[0035] A gas source tank 5 for supplying carbon dioxide gas and having a gas outlet. The gas source tank 5 comprises a high-concentration carbon dioxide cylinder 503, a gas pressure reducing valve 501, and a gas source on/off ball valve 502. A pipeline is connected to the top of the high-concentration carbon dioxide cylinder 503. The pipeline near the outlet is equipped with a gas source on/off ball valve 502 and a gas pressure reducing valve 501. The gas outlet of the gas source tank 5 is the outlet of the pipeline to which the gas source tank 5 is connected. A gas booster pump assembly is connected to the gas outlet (pipeline output) via a pipeline. The gas booster pump assembly is connected to the delivery pipe. The gas booster pump assembly ensures that the carbon dioxide delivered into the corrosion vessel 1 reaches a supercritical pressure of 7.38 MPa. The gas booster pump assembly includes a gas booster pump 4, which comprises a booster cylinder 401 and a drive cylinder 402. One end of the booster cylinder 401 is connected to the drive cylinder 402. One end of the drive cylinder 402 is provided with a low-pressure air inlet 403, which is connected to the gas source storage tank 5 via a third inlet pipe 404. The drive cylinder 402 is provided with a high-pressure air outlet 405, which is connected to the delivery pipe via a second inlet pipe 305. Specifically, the gas booster pump assembly includes the gas booster pump 4 and a buffer vessel 3. The buffer vessel 3 is located between the gas booster pump 4 and the corrosion vessel 1. The air inlet of the buffer vessel 3 is connected to the gas booster pump 4 via a pipeline, and the air outlet of the buffer vessel 3 is connected to the corrosion vessel 1 via a delivery pipe. Buffer vessel 3 comprises a pressure buffer tank 301, a first high-pressure interface screw 302, a high-pressure gas three-way valve 303, a second high-pressure interface screw 304, and a second inlet pipe 305. The top outlet of the pressure buffer tank 301 is connected to a pipeline via the first high-pressure interface screw 302, which is connected to one outlet of the high-pressure gas three-way valve 303. The second high-pressure interface screw 304 is located at one inlet of the high-pressure gas three-way valve 303 and is threadedly connected to the second inlet pipe 305. The other outlet of the high-pressure gas three-way valve 303 is connected to the corrosion vessel 1 via a delivery pipe. Specifically, both the corrosion vessel 1 and the buffer vessel 3 are made of a high-temperature, pressure-resistant, and corrosion-resistant alloy. This ensures that the materials of the buffer vessel 3 and the corrosion vessel 1 themselves are not corroded by CO2 during long-term corrosion testing, which would otherwise contaminate the specimens with corrosion products. Both the buffer vessel 3 and the corrosion vessel 1 are made of a high-temperature, corrosion-resistant alloy, alloy numbered GH4161. Specifically, the delivery pipe is equipped with a pressure gauge and a needle-type pressure control valve for adjusting the CO2 pressure. The pressure gauge includes a first pressure gauge 102 and a second pressure gauge 205, and the needle pressure control valve includes a first needle pressure regulating valve 103 and a second needle pressure regulating valve 204. This is intended to ensure that the buffer vessel 3 and corrosion vessel 1 materials themselves are not corroded by CO2 during long-term corrosion testing, which would otherwise cause corrosion products from the metal materials to contaminate the specimen. Both the buffer vessel 3 and corrosion vessel 1 are made of a high-temperature corrosion-resistant alloy, alloy number GH4161. Specifically, the corrosion vessel 1 comprises two independent upper and lower first and second corrosion chambers, each containing a saturated carbon dioxide solution. At least two rock sample racks are provided, one in each of the first and second corrosion chambers. The sealing covers comprise a first sealing cover 2 and a second sealing cover 101. The first sealing cover 2 is threadedly connected to the top opening of the first corrosion chamber, while the second sealing cover 101 is threadedly connected to the bottom opening of the second corrosion chamber. The delivery pipe comprises a transmission pipe and a transmission pipe, both of which are connected to the gas booster pump assembly via pipelines. The transmission pipe is connected to the high-pressure gas screw interface 207 at the end of the first inlet pipe 206, passes through the first sealing cover 2, and connects to the first corrosion chamber. The transmission pipe is connected to the second corrosion chamber. The first inlet pipe 206 is also connected to a second needle pressure regulating valve 204 and a second pressure gauge 205, while the transmission pipe is also connected to the first needle pressure regulating valve 103 and a first pressure gauge 102. Specifically, the first sealing cover 2 has a first sealing body 201 threadedly connected to the first corrosion chamber, and the second sealing cover 101 has a second sealing body threadedly connected to the second corrosion chamber. A first sealing ring 202 and a second sealing ring 203 are sleeved above and below the first sealing body 201 and the second sealing body. Specifically, the distance between the first sealing ring 202 and the second sealing ring 203 is 5 cm to 5.2 cm. The first sealing ring 202 is positioned in the middle of the first sealing body 201 or the second sealing body, and the second sealing ring 203 is positioned at the threaded end of the first sealing body 201 or the second sealing body, to provide a tighter connection between the first sealing cover 2 and the first corrosion chamber, or between the second sealing cover 101 and the second corrosion chamber. Specifically, all pipelines have threaded connections at the inlet and outlet ends, and all pipelines are covered with polytetrafluoroethylene (PTFE) wire. The threads at the pipeline connections ensure connection and replacement if damaged. The PTFE wire protects the pipelines from CO2 corrosion and is also wear-resistant. The present invention provides a method for using a supercritical carbon dioxide rock corrosion experimental system, comprising the following steps: Place a rock sample on a rock sample holder, and fill a corrosion vessel 1 with a saturated carbon dioxide aqueous solution so that the lower portion of the rock sample is immersed in the saturated carbon dioxide aqueous solution; Then, open a gas source tank 5, and pump the carbon dioxide in the gas source tank 5 into a gas booster pump 4 for pressurization. The pressurized carbon dioxide is then delivered to the corrosion vessel 1 through a delivery pipe. A controller 6 controls the heating temperature of a heating component to convert the pressurized carbon dioxide gas delivered to the corrosion vessel 1 into supercritical carbon dioxide, thereby placing the rock sample on the rock sample holder in a supercritical and liquid phase environment. Controller 6 includes a temperature controller 601 connected to a resistance heating element 602 for providing a constant temperature heat source for the corrosion vessel 1. The heating element is a resistance heating element 602. The desired temperature is set by the temperature controller 601, and the resistance heating element 602 provides a stable temperature. It is apparent that those skilled in the art may make various modifications and variations to the present invention without departing from the spirit and scope of the present invention. Thus, if these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is intended to include these modifications and variations.	Family Number\|(115489354)\|115489354\|Advantages / Prev. Drawbacks\|(CN120404566 A)\|In a carbon dioxide geological sequestration environment , rock - supercritical carbon dioxide - carbon dioxide groundwater solutions are in coexistence , supercritical carbon ( . . . ) physical and chemical properties of the rock , while carbon dioxide groundwater solutions can react with certain minerals in the rock ( such as silicate ) , which may generate new mineral phases , which may have different physical and chemical properties , thereby affecting the properties of the rock , so that it is necessary to study the rock properties while supercritical carbon dioxide - carbon ( . . . ) \|(CN120404566B B)\|In a carbon dioxide geological sequestration environment , rock - supercritical carbon dioxide - carbon dioxide groundwater solutions are in coexistence , supercritical carbon ( . . . ) physical and chemical properties of the rock , while carbon dioxide groundwater solutions can react with certain minerals in the rock ( such as silicate ) , which may generate new mineral phases , which may have different physical and chemical properties , thereby affecting the properties of the rock , so that it is necessary to study the rock properties while supercritical carbon dioxide - carbon ( . . . ) \|	Analysis of biological materials\|Measurement	G01N-017/00\|G01N-017/00/2\|G01N-017/00/4\|G01N-017/00/6\|G01N-033/24		G01N-017/00\|G01N-017/00/2\|G01N-017/00/4\|G01N-017/00/6\|G01N-033/24	G01N-017/00\|G01N-033/24	G01N-017/00\|G01N-033/24					CN119959123\|CN119715348\|CN212844929U\|CN206863025U\|CN118226006\|CN112326484	CN119959123 114498188 WHO=Examiner SELF=N CAT=A\|CN119715348 113968326 WHO=Examiner SELF=Y CAT=A\|CN212844929U 93388591 WHO=Examiner SELF=N CAT=A\|CN206863025U 78357085 WHO=Examiner SELF=Y CAT=A\|CN118226006 110304989 WHO=Examiner SELF=N\|CN112326484 92618298 WHO=Examiner SELF=N		\|CN206863025U; CN212844929U; CN119715348; CN119959123; CN118226006; CN112326484		GRANTED	(US20260104346)\|PENDING\|(CN120404566)\|GRANTED	ALIVE	(US20260104346)\|ALIVE\|(CN120404566)\|ALIVE	(US20260104346)\|LEGAL DETAILS FOR US20260104346\|Actual or expected expiration date=2045-12-15\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-12-15\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19420413\|Application date=2025-12-15\|Standardized application number=2025US-19420413\|Event publication date=2026-04-16\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20260104346\|Publication stage code=A1\|Publication date=2026-04-16\|Standardized publication number=US20260104346\|(CN120404566)\|LEGAL DETAILS FOR CN120404566\|Actual or expected expiration date=2045-07-07\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2025-07-07\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202510926442\|Application date=2025-07-07\|Standardized application number=2025CN-0926442\|Event publication date=2025-08-01\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN120404566\|Publication stage code=A\|Publication date=2025-08-01\|Standardized publication number=CN120404566\|Event publication date=2025-08-01\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2025-08-19\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2025-09-05\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN120404566\|Publication stage code=B\|Publication date=2025-09-05\|Standardized publication number=CN120404566B\|Event publication date=2025-09-05\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right		(US20260104346)\|US\|(CN120404566)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcMs4KvXHfo1KF90CpEah8ymJjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023424804&ekey=1966&xpn=US20260104346&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19420413/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=%252F4P%252Bo1Atd%252FXzAir%252FMtFSLMRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	CN	(US20260104346)\|CN\|(CN120404566)\|CN\|(CN120404566)\|CN	(US20260104346)\|NAME=Shaoxing University , CITY=Shaoxing City , COUNTRY=CN , ATYP=Non-US Company NAME=China University of Mining and Technology , CITY=Xuzhou , COUNTRY=CN , ATYP=Non-US Company\|(CN120404566)\|NAME=CHINA UNIVERSITY OF MINING & TECHNOLOGY , COUNTRY=CN\|(CN120404566)\|NAME=CHINA UNIVERSITY OF MINING & TECHNOLOGY , COUNTRY=CN		(CN120404566)\|NAME=JI LI;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223\|(CN120404566)\|NAME=JI LI;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223	(US20260104346)\|CN; CN; CN; CN; CN; CN\|(CN120404566)\|CN\|(CN120404566)\|CN	(US20260104346)\|NAME=YANG Shengqi, CITY=Shaoxing City, COUNTRY=CN \|NAME=LI Yue, CITY=Shaoxing City, COUNTRY=CN \|NAME=HUANG Yanhua, CITY=Shaoxing City, COUNTRY=CN \|NAME=YIN Pengfei, CITY=Shaoxing City, COUNTRY=CN \|NAME=TIAN Wenling, CITY=Shaoxing City, COUNTRY=CN \|NAME=ZHU Zhennan, CITY=Shaoxing City, COUNTRY=CN\|(CN120404566)\|NAME=YANG SHENGQI, COUNTRY=CN \|NAME=LI YUE\|NAME=HUANG YANHUA\|NAME=YIN PENGFEI\|NAME=TIAN WENLING\|NAME=ZHU ZHENNAN\|(CN120404566)\|NAME=YANG SHENGQI, COUNTRY=CN \|NAME=LI YUE\|NAME=HUANG YANHUA\|NAME=YIN PENGFEI\|NAME=TIAN WENLING\|NAME=ZHU ZHENNAN	(US20260104346)\|8\|(CN120404566)\|8	1	2					(US20260104346)\|Number of Claims: NCL=8\|Number of Drawings: NDR=8\|Number of Figures: NFG=8\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|\|(CN120404566)\|Number of Claims: NCL=8\|Gazette date: GAZDATE=2025-09-05\|Gazette number: GAZNUM=41-3602\|Substantial examination effective date: 20250819 Examination duration: 0 months\|Number of Pages: NPAGES=15\|Primary examiner: 韩莉莉\|Primary examiner: Han Lili\|\|(CN120404566)\|Number of Claims: NCL=9\|Gazette date: GAZDATE=2025-08-01\|Gazette number: GAZNUM=41-3102\|Number of Pages: NPAGES=15\|Primary examiner: 韩莉莉\|Primary examiner: Han Lili\|	(CN120404566)\|Previous publication: CN120404566 A 2025-08-01 [CN120404566]	(US20260104346)\|ENGLISH (ENG)	(US20260104346)\|Patent\|(CN120404566B)\|Patent\|(CN120404566)\|Patent	Titre: (US20260104346)\|An Experimental System for Rock Corrosion by Supercritical Carbon Dioxide Résumé: (US20260104346)\|The present invention relates to an experimental system and usage method for supercritical carbon dioxide rock corrosion. The experimental system comprises a corrosion vessel for exposing samples to a saturated carbon dioxide aqueous solution. The inside of the corrosion vessel is provided with a heating assembly and a rock sample placement rack. The top of the rock sample placement rack is above the liquid level of saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is submerged in saturated carbon dioxide aqueous solution. The heating assembly is located on the perimeter wall of the corrosion vessel and connected with a controller. The corrosion vessel is connected to a carbon dioxide gas delivery unit and a booster pump assembly connected via a conveying pipe. The present invention enables rocks to corrode in both supercritical and carbon dioxide solutions.	40	Abstract	gpt-4o-mini	no	The focus is on an experimental system for rock corrosion using supercritical CO₂, not on accelerating mineral weathering for CO₂ capture.
42	US61/152,146P\|US61/152,146\|US12/703,560\|WOUS2010/023874	VE2010-000232\|WOUS2010/023874\|MA34158\|IN1891/MUMNP/2011\|ZA201106555\|EG2011081356\|TN2011000392\|IL214550\|BRPI1008552\|CN201080016465\|EP10741714\|MX2011008534\|UAA201110794\|AU2010213774\|EA201171025\|AP201105875\|CA2752133\|MYPI2011003744\|PE2011001479\|US12/703,560	VE2010000232\|BRPI1008552\|CN102395653\|MY152426\|EP2406351\|MX320012\|UA104617\|EG26419\|AU2010213774\|TN2011000392\|US8349171\|BRPI1008552\|VE2010000232\|PE20120707\|ZA201106555\|CN102395653\|MA33113\|EA201171025\|IN1891/MUMNP/2011\|EP2406351\|MX2011008534\|AP2011005875\|AP201105875\|IL214550\|AU2010213774\|WO2010/093777\|CA2752133\|WO2010/093777\|US20100200467	35292	VE2010000232 B 2021-12-13 [VE2010000232]\|VE2010000232 A 2012-07-26 [VE2010000232]\|WO2010/093777 A3 2010-12-09 [WO201093777]\|WO2010/093777 A2 2010-08-19 [WO201093777]\|MA33113 B1 2012-03-01 [MA--33113]\|IN1891/MUMNP/2011 A 2012-02-03 [IN2011MN01891]\|ZA201106555 B 2012-05-30 [ZA201106555]\|EG26419 A 2013-10-23 [EG--26419]\|TN2011000392 A1 2013-03-27 [TN2011000392]\|IL214550 A 2011-09-27 [IL-214550]\|BRPI1008552 A2 2016-03-15 [BR201008552]\|BRPI1008552 A0 2012-11-20 [BR201008552]\|CN102395653 B 2015-05-06 [CN102395653B]\|CN102395653 A 2012-03-28 [CN102395653]\|EP2406351 A4 2014-09-17 [EP2406351]\|EP2406351 A2 2012-01-18 [EP2406351]\|MX320012 B 2014-05-05 [MX-320012]\|MX2011008534 A 2011-12-16 [MX2011008534]\|UA104617 C2 2014-02-25 [UA-104617]\|AU2010213774 B2 2013-06-13 [AU2010213774]\|AU2010213774 A1 2011-09-22 [AU2010213774]\|EA201171025 A1 2012-02-28 [EA201171025]\|AP201105875 D0 2011-10-31 [AP201105875]\|AP2011005875 A0 2011-10-31 [AP2011005875]\|CA2752133 A1 2010-08-19 [CA2752133]\|MY152426 A 2014-09-30 [MY-152426]\|PE20120707 A1 2012-06-27 [PE201200707]\|US8349171 B2 2013-01-08 [US8349171]\|US20100200467 A1 2010-08-12 [US20100200467]	2009-02-12\|2010-02-10\|2010-02-11	2010-02-12\|2010-02-11\|2011-09-09\|2011-09-09\|2011-09-07\|2011-08-11\|2011-08-09\|2011-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-10	2021-12-13\|2016-03-15\|2015-05-06\|2014-09-30\|2014-09-17\|2014-05-05\|2014-02-25\|2013-10-23\|2013-06-13\|2013-03-27\|2013-01-08\|2012-11-20\|2012-07-26\|2012-06-27\|2012-05-30\|2012-03-28\|2012-03-01\|2012-02-28\|2012-02-03\|2012-01-18\|2011-12-16\|2011-10-31\|2011-10-31\|2011-09-27\|2011-09-22\|2010-12-09\|2010-08-19\|2010-08-19\|2010-08-12	\|(US8349171)\|2013-01-08\|\|(CN102395653B)\|2015-05-06\|(VE2010000232)\|2021-12-13\|(MY-152426)\|2014-09-30\|(MX-320012)\|2014-05-05\|(UA-104617)\|2014-02-25\|(EG--26419)\|2013-10-23\|(AU2010213774)\|2013-06-13\|(ZA201106555)\|2012-05-30\|(MA--33113)\|2012-03-01\|\|\|\|\|\|\|\|	(EP2406351)\|2015-03-20\|(US8349171)\|2025-02-10\|(WO2010/093777)\|2012-08-12\|(CN102395653)\|2016-02-11\|(VE2010000232)\|2030-02-12\|(MY152426)\|2030-02-11\|(MX320012)\|2030-02-11\|(UA104617)\|2030-02-11\|(EG26419)\|2030-02-11\|(AU2010213774)\|2016-09-08\|(ZA201106555)\|2030-02-11\|(MA33113)\|2030-02-11\|(BRPI1008552)\|2016-09-13\|(TN2011000392)\|2030-02-11\|(PE20120707)\|2016-01-29\|(EA201171025)\|2017-02-28\|(IN1891/MUMNP/2011)\|2022-02-03\|(AP201105875)\|2016-10-31\|(IL214550)\|2016-09-27\|(CA2752133)\|2016-02-11	(EP2406351)\|Methods of recovering hydrocarbons from hydrocarbonaceous material using a constructed infrastructure and associated systems maintained under positive pressure	(EP2406351)\|A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure (100). This constructed infrastructure (100) defines a substantially encapsulated volume. A comminuted hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body (120) of hydrocarbonaceous material. The permeable body (120) can be heated sufficient to remove hydrocarbons therefrom. During heating and removal of hydrocarbons and subsequent thereto a positive pressure can be maintained within the encapsulated volume by means of a non-oxidizing gas to expedite flushing of hydrocarbonaceous material, inhibit unwanted entry of oxygen into the encapsulated volume and remove recoverable hydrocarbons following the heating process.	RED LEAF RESOURCES	(EP2406351)\|Red Leaf Resources, Inc. ([US])\|(EP2406351)\|Red Leaf Resources, Inc. ([US])\|(US8349171)\|Red Leaf Resources, Inc. ([US])\|(US20100200467)\|DANA TODD\|PATTEN JAMES W\|(WO2010/093777)\|RED LEAF RESOURCES, INC.\|(WO2010/093777)\|RED LEAF RESOURCES, INC. ([US])\|(CN102395653)\|RED LEAF RESOURCES INC. ([US])\|(CN102395653)\|RED LEAF RESOURCES INC. ([US])\|\|\|(MY152426)\|RED LEAF RESOURCES, INC.\|(MX320012)\|RED LEAF RESOURCES INC* ([US])\|(MX2011008534)\|RED LEAF RESOURCES INC*\|(UA104617)\|RED LEAF RESOURCES, INC.\|(EG26419)\|RED LEAF RESOURCES INC\|(AU2010213774)\|Red Leaf Resources, Inc.\|(AU2010213774)\|Red Leaf Resources, Inc.\|(ZA201106555)\|RED LEAF RESOURCES INC\|(MA33113)\|RED LEAF RESOURCES, INC.\|(BRPI1008552)\|RED LEAF RESOURCES, INC.\|\|(TN2011000392)\|RED LEAF RESOURCES, INC.\|(PE20120707)\|RED LEAF RESOURCES, INC.\|\|(IN1891/MUMNP/2011)\|RED LEAF RESOURCES INC ([US])\|\|(AP2011005875)\|RED LEAF RESOURCES INC\|(IL214550)\|RED LEAF RESOURCES, INC\|(CA2752133)\|RED LEAF RESOURCES, INC. ([US])	DANA TODD\|PATTEN JAMES W	(EP2406351)\|DANA, Todd\|PATTEN, James, W.\|(EP2406351)\|DANA, Todd\|PATTEN, James, W.	(EP2406351)\|Walker, Ross Thomson;Forresters ([DE])\|Reg. Nb: 101298687\|(US8349171)\|Thorpe North & Western LLP\|(WO2010/093777)\|Ericksen Erik S. et al. ([US])\|(CN102395653)\|ZHAO RONGMIN;JEEKAI & PARTNERS\|Reg. Nb: 11245\|(VE2010000232)\|LINARES ALLOCA MARLIN ENEIDA\|(MX320012)\|MARIA ANGELICA PARDAVELL JUAREZ\|(AU2010213774)\|FB Rice ([AU])\|(CA2752133)\|BERESKIN & PARR LLP/S.E.N.C.R.L.,S.R.L. ([CA])	(US8349171)\|As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required.\|Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|In some cases it can be desirable to provide a single type of hydrocarbonaceous material so that the permeable body consists essentially of one of the above materials.\|In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants. This approach uniquely provides solutions to problems for not just one, but many problems, and in an integrated approach.\|More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body.\|Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like.\|	(US8349171)\|1. A method of recovering hydrocarbons from hydrocarbonaceous materials, comprising: a) forming a constructed permeability control infrastructure which defines a substantially encapsulated volume; b) introducing a comminuted hydrocarbonaceous material into the control infrastructure to form a permeable body of hydrocarbonaceous material; c) maintaining within said encapsulated volume a positive pressure relative to the pressure outside of said control infrastructure; d) heating the hydrocarbonaceous material sufficient to remove hydrocarbons therefrom such that the hydrocarbonaceous material is substantially stationary during heating; e) flushing a gaseous fluid substantially free of oxygen throughout the permeable body in order to substantially remove hydrocarbons and other gaseous components from the permeable body, wherein heating of said hydrocarbonaceous materials has been terminated and said gaseous fluid is passed throughout the permeable body at a low temperature relative to the temperature at which said hydrocarbonaceous materials have been heated to provide a cooling effect on said hydrocarbonaceous materials and flush residual hydrocarbons and other gaseous materials from within said encapsulated volume; and f) collecting removed hydrocarbons and other gaseous components.\|16. A constructed permeability control infrastructure, comprising: a) a permeability control impoundment defining a substantially encapsulated volume, said impoundment having a foundation structural floor support of earthen material or local surface topography as a floor; and b) a comminuted hydrocarbonaceous material within the encapsulated volume forming a substantially stationary permeable body of hydrocarbonaceous material, wherein the impoundment is adapted such that a positive pressure is maintained in said encapsulated volume relative to the pressure outside of said control infrastructure and prevents the introduction of air or other oxidizing gases from entering the impoundment.\|	(US8349171)\|In another aspect, walls of the impoundment can be acid, water and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water.\|In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|In yet another detailed aspect, the permeable body can further comprise an additive or biomass.\|	(US8349171)\|HYDROCARBONACEOUS MATERIAL(100,43)\|INFRASTRUCTURE(100,25)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|CONSTRUCTED PERMEABILITY(100,16)\|POSITIVE PRESSURE(100,15)\|RECOVERING HYDROCARBON(100,12)\|ENCAPSULATED VOLUME(91,25)\|FOUNDATION FLOOR STRUCTURE(76,2)\|FLUSH RESIDUAL HYDROCARBON(69,1)\|BENTONITE CLAY(67,5)\|GASEOUS FLUID(63,4)\|ATMOSPHERIC POLLUTANT(58,1)\|GASEOUS COMPONENT(54,2)\|GEOTEXTILE BAG(53,3)\|IMPOUNDMENT(52,65)\|SOLVENT RECOVERY(52,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(51,6)\|CLAY LINING(49,1)\|ACID HALIDE(47,1)\|RESIN ION EXCHANGE(47,1)\|METHANEDIONE PRODUCTION(46,1)\|SYNTHETIC GEOGRID(45,3)\|OIL SHALE ORE(42,1)\|CARBONATE DECOMPOSITION(41,2)\|SYNTHETIC CLAY(40,1)\|ENORMOUS VOLUME CAPACITY(39,1)\|COLLECTING REMOVED HYDROCARBON(37,1)\|CO2 EMISSION(36,2)\|CONTROL INFRASTRUCTURE(35,22)\|OXIDIZING GAS(35,2)\|TEMPERATURE GEOMEMBRANE(35,1)\|SOLUTION MINING(33,1)\|REFRACTORY CEMENT(32,6)\|POLYMERIC RESIN(32,3)\|PERMEABILITY(31,24)\|BRINE SOLUTION(31,1)\|ELECTROPLATING(31,1)\|EXTRACT FLUID(31,1)\|REBAR(29,5)\|FLOTATION(29,1)\|IMPOUNDMENT WALL(28,12)\|LEACHING(28,1)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|GASEOUS MATERIAL(27,3)\|GUIDELINE(26,4)\|PERMEABILITY CONTROL IMPOUNDMENT(26,4)\|HYDROCARBON COMBUSTION(26,3)\|HYDROCARBONACEOUS MATERIAL FLUSHING(26,1)\|FIBERGLASS(23,5)\|BRINE(23,1)\|PRECIPITATION(22,2)\|EARTHEN MATERIAL(21,4)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|VOID SPACE(20,5)\|SEALANT(20,2)\|MALFUNCTION(20,1)\|BIOMASS(19,3)\|SECTIONED CAPSULE IMPOUNDMENT(19,2)\|ADDITIVE(18,13)\|STOICHIOMETRIC CONDITION(18,3)\|TOTAL VOLUME(18,2)\|COMPACTED FILL CEILING(17,3)\|GROUT(17,3)\|DRAIN PIPE(17,1)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(17,1)\|MECHANICAL INTEGRITY(17,1)\|HYDRO CARBONACEOUS DEPOSIT EXCAVATION(16,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(16,1)\|RESISTANCE HEATER(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|INFRASTRUCTURE OPERATING TEMPERATURE(15,1)\|QUARRY CAPSULE IMPOUNDMENT(15,1)\|UNCAPPED CAPSULE IMPOUNDMENT(15,1)\|UNDERGROUND RUBBLE CHIMNEY(15,1)\|EXTRACTION(14,2)\|NANOCARBON FULLERENE ADDITIVE(14,1)\|STRUCTURED IMPOUNDMENT CAPSULE(14,1)\|HYDROCARBON PRODUCTION(13,12)\|PROPANE(12,6)\|CONTAINMENT CAPSULE(12,2)\|NEARBY IMPOUNDMENT(12,2)\|TAILING BERM(12,2)\|UNRECOVERED HYDROCARBON(12,2)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|COAL(11,7)\|PEAT(11,4)\|ECONOMIC VALUE(11,1)\|ENGINEERED PERMEABILITY BARRIER(11,1)\|HYDROCARBON LEAN SHALE(11,1)\|HYDROCARBON UNCONTROLLED EGRESS(11,1)\|UNDERGROUND MINED HYDROCARBON(11,1)\|VOID VOLUME(10,7)\|FUEL CELL(10,5)\|RADIO FREQUENCY(10,4)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|BENCH MINING ELEVATION(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|ECONOMICALLY COMPETITIVE RECOVERY(10,1)\|EXTERIOR CAPSULE IMPOUNDMENT(10,1)\|GARBAGE IMPOUNDMENT(10,1)\|GRAVITY ASSISTED DRAINAGE PIPE(10,1)\|GRAVITY DRAINAGE ASSISTANCE(10,1)\|INDISCRIMINATE DUMPING(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|MANIPULATED GRADE SHALE(10,1)\|MEDIAN SIZE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|UNTAPPED RESOURCE(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|HEAT PIPE(9,6)\|CONSTRUCTED SULFUR CAPSULE(9,2)\|IMPOUNDMENT HEIGHT(9,2)\|PRECIOUS METAL(8,5)\|IMPERMEABLE FLOOR LAYER(8,3)\|SURFACE TOPOGRAPHY(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CORE DRILLING(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|HYDROCARBONACEOUS DEPOSIT(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MINING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|LIQUID PRODUCT(7,11)\|HYDRO CARBONACEOUS MATERIAL(7,4)\|CONVECTIVE HEATING(7,2)\|CRUSHED GLASS(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HEATED CONDUIT(7,2)\|HEATING(7,2)\|HORIZONTAL MINING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|BIO LEACHING(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HEATING RESIDENCE TIME(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PERMEABILITY BALANCE(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|HEAT TRANSFER(6,10)\|HYDROGEN DONOR(6,7)\|HEAVY METAL(6,5)\|BLASTING(6,3)\|CONVECTION(6,3)\|FREEZE WALL(6,3)\|ECONOMICS(6,2)\|FLOOR CONSTRUCTION(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENCLOSED CAPSULE(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MAXIMIZE RECOVERY(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|KEROGEN OIL(5,4)\|HEATED FLUID(5,3)\|PIPING(5,3)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|ANAEROBIC CONDITION(5,1)\|AQUEOUS SLURRY(5,1)\|BARRIER MANUFACTURE(5,1)\|CAPACITY INDICATOR(5,1)\|CAPSULE IMPOUNDMENT AREA(5,1)\|CATALYZING GAS(5,1)\|CEILING CAP(5,1)\|CLAY PIPE(5,1)\|CO2 PRODUCTION(5,1)\|COMMINUTED MASS(5,1)\|COMPOSITION ADMIXTURE(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|DECREASED VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLUID DRAINAGE(5,1)\|FLUSHING GAS(5,1)\|FUTURE DATE(5,1)\|GAS COMBUSTION HEATER(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GASEOUS LIGHT HYDROCARBON(5,1)\|GEO MEMBRANE LAYER(5,1)\|GEO SYNTHETIC MEMBRANE(5,1)\|GEOLOGICAL LOCATION(5,1)\|HEATING CONDUIT PLACEMENT(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|IMPOUNDMENT USEFUL LIFE(5,1)\|INORGANIC MATTER(5,1)\|KEROGEN REMOVAL(5,1)\|LAYER COMPACTION(5,1)\|LONG HEATING RESIDENCE TIME(5,1)\|MICROBIOLOGY(5,1)\|MINIMAL WASTE(5,1)\|MINING HAUL TRUCK NEED(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONOXIDIZING GAS(5,1)\|OIL BLEND(5,1)\|OPTIMIZATION REASON(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|PRECAST PIECE(5,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(5,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(5,1)\|QUALITY DETERIORATION(5,1)\|RECOVERED HYDROCARBON LIQUID(5,1)\|RECOVERING OIL(5,1)\|REFORMATION(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RESIDUAL SHALE REDUCED WETTING(5,1)\|RICH OIL BEARING ORE(5,1)\|ROTATING RETORT(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT CLOSER(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|STAGED PROCESSING(5,1)\|STEAM INJECTION(5,1)\|TECHNICAL CHALLENGE(5,1)\|TREMENDOUS VOLUME(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNCONTROLLED MIGRATION PREVENTION(5,1)\|VAPOROUS COMPONENT(5,1)\|VARIED ENZYME(5,1)\|VOLATILE ORGANIC(5,1)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOMATERIAL(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DIFFICULT CHALLENGE(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|FUNCTION VOID SPACE(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|\|(US20100200467)\|HYDROCARBONACEOUS MATERIAL(100,42)\|INFRASTRUCTURE(100,22)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,15)\|CONSTRUCTED PERMEABILITY(100,12)\|RECOVERING HYDROCARBON(100,12)\|ENCAPSULATED VOLUME(87,25)\|GASEOUS FLUID(60,5)\|ATMOSPHERIC POLLUTANT(58,1)\|GASEOUS COMPONENT(54,2)\|SOLVENT RECOVERY(52,2)\|COMMINUTED HYDRO CARBONACEOUS MATERIAL(51,1)\|CLAY LINING(49,1)\|ACID HALIDE(47,1)\|RESIN ION EXCHANGE(47,1)\|METHANEDIONE PRODUCTION(46,1)\|OIL SHALE ORE(42,1)\|BENTONITE CLAY(41,3)\|CARBONATE DECOMPOSITION(41,2)\|SYNTHETIC CLAY(40,1)\|ENORMOUS VOLUME CAPACITY(39,1)\|FLUSH RESIDUAL HYDROCARBON(39,1)\|FLUSH HYDROCARBON VAPOR(38,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(37,5)\|COLLECTING REMOVED HYDROCARBON(37,1)\|CO2 EMISSION(36,2)\|CONTROL INFRASTRUCTURE(35,22)\|TEMPERATURE GEOMEMBRANE(35,1)\|SOLUTION MINING(33,1)\|PERMEABILITY(31,24)\|BRINE SOLUTION(31,1)\|ELECTROPLATING(31,1)\|EXTRACT FLUID(31,1)\|FLOTATION(29,1)\|IMPOUNDMENT WALL(28,12)\|LEACHING(28,1)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|GUIDELINE(26,4)\|PERMEABILITY CONTROL IMPOUNDMENT(26,4)\|HYDROCARBON COMBUSTION(26,3)\|HYDROCARBONACEOUS MATERIAL FLUSHING(26,1)\|HYDRO CARBONACEOUS MATERIAL(23,5)\|BRINE(23,1)\|GASEOUS MATERIAL(22,3)\|PRECIPITATION(22,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|VOID SPACE(20,5)\|SEALANT(20,2)\|MALFUNCTION(20,1)\|REFRACTORY CEMENT(19,4)\|BIOMASS(19,3)\|SECTIONED CAPSULE IMPOUNDMENT(19,2)\|ADDITIVE(18,13)\|STOICHIOMETRIC CONDITION(18,3)\|TOTAL VOLUME(18,2)\|COMPACTED FILL CEILING(17,3)\|GROUT(17,3)\|REBAR(17,3)\|DRAIN PIPE(17,1)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(17,1)\|MECHANICAL INTEGRITY(17,1)\|HYDRO CARBONACEOUS DEPOSIT EXCAVATION(16,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(16,1)\|RESISTANCE HEATER(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|HEATED HYDROCARBONACEOUS MATERIAL(15,1)\|INFRASTRUCTURE OPERATING TEMPERATURE(15,1)\|QUARRY CAPSULE IMPOUNDMENT(15,1)\|UNCAPPED CAPSULE IMPOUNDMENT(15,1)\|UNDERGROUND RUBBLE CHIMNEY(15,1)\|EXTRACTION(14,2)\|NANOCARBON FULLERENE ADDITIVE(14,1)\|STRUCTURED IMPOUNDMENT CAPSULE(14,1)\|HYDROCARBON PRODUCTION(13,12)\|PROPANE(12,6)\|CONTAINMENT CAPSULE(12,2)\|NEARBY IMPOUNDMENT(12,2)\|TAILING BERM(12,2)\|UNRECOVERED HYDROCARBON(12,2)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|COAL(11,7)\|PEAT(11,4)\|ECONOMIC VALUE(11,1)\|ENGINEERED PERMEABILITY BARRIER(11,1)\|HYDROCARBON LEAN SHALE(11,1)\|HYDROCARBON UNCONTROLLED EGRESS(11,1)\|UNDERGROUND MINED HYDROCARBON(11,1)\|VOID VOLUME(10,7)\|FUEL CELL(10,5)\|RADIO FREQUENCY(10,4)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|BENCH MINING ELEVATION(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|ECONOMICALLY COMPETITIVE RECOVERY(10,1)\|EXTERIOR CAPSULE IMPOUNDMENT(10,1)\|GARBAGE IMPOUNDMENT(10,1)\|GRAVITY ASSISTED DRAINAGE PIPE(10,1)\|GRAVITY DRAINAGE ASSISTANCE(10,1)\|INDISCRIMINATE DUMPING(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|MANIPULATED GRADE SHALE(10,1)\|MEDIAN SIZE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|UNTAPPED RESOURCE(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|HEAT PIPE(9,6)\|CONSTRUCTED SULFUR CAPSULE(9,2)\|IMPOUNDMENT HEIGHT(9,2)\|PRECIOUS METAL(8,5)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CORE DRILLING(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|HYDROCARBONACEOUS DEPOSIT(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MINING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|LIQUID PRODUCT(7,11)\|CONVECTIVE HEATING(7,2)\|CRUSHED GLASS(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HEATED CONDUIT(7,2)\|HEATING(7,2)\|HORIZONTAL MINING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|BIO LEACHING(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HEATING RESIDENCE TIME(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PERMEABILITY BALANCE(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|HEAT TRANSFER(6,10)\|HYDROGEN DONOR(6,7)\|HEAVY METAL(6,5)\|BLASTING(6,3)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|ECONOMICS(6,2)\|FLOOR CONSTRUCTION(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENCLOSED CAPSULE(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MAXIMIZE RECOVERY(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|KEROGEN OIL(5,4)\|HEATED FLUID(5,3)\|PIPING(5,3)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|ANAEROBIC CONDITION(5,1)\|AQUEOUS SLURRY(5,1)\|BARRIER MANUFACTURE(5,1)\|CAPACITY INDICATOR(5,1)\|CAPSULE IMPOUNDMENT AREA(5,1)\|CATALYZING GAS(5,1)\|CEILING CAP(5,1)\|CLAY PIPE(5,1)\|CO2 PRODUCTION(5,1)\|COMMINUTED MASS(5,1)\|COMPOSITION ADMIXTURE(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|DECREASED VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLUID DRAINAGE(5,1)\|FLUSHING GAS(5,1)\|FUTURE DATE(5,1)\|GAS COMBUSTION HEATER(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GASEOUS LIGHT HYDROCARBON(5,1)\|GEO MEMBRANE LAYER(5,1)\|GEO SYNTHETIC MEMBRANE(5,1)\|GEOLOGICAL LOCATION(5,1)\|HEATING CONDUIT PLACEMENT(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|IMPOUNDMENT USEFUL LIFE(5,1)\|INORGANIC MATTER(5,1)\|KEROGEN REMOVAL(5,1)\|LAYER COMPACTION(5,1)\|LONG HEATING RESIDENCE TIME(5,1)\|MICROBIOLOGY(5,1)\|MINIMAL WASTE(5,1)\|MINING HAUL TRUCK NEED(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONOXIDIZING GAS(5,1)\|OIL BLEND(5,1)\|OPTIMIZATION REASON(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PRECAST PIECE(5,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(5,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(5,1)\|QUALITY DETERIORATION(5,1)\|RECOVERED HYDROCARBON LIQUID(5,1)\|RECOVERING OIL(5,1)\|REFORMATION(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RESIDUAL SHALE REDUCED WETTING(5,1)\|RICH OIL BEARING ORE(5,1)\|ROTATING RETORT(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|STAGED PROCESSING(5,1)\|STEAM INJECTION(5,1)\|TECHNICAL CHALLENGE(5,1)\|TREMENDOUS VOLUME(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNCONTROLLED MIGRATION PREVENTION(5,1)\|VAPOROUS COMPONENT(5,1)\|VARIED ENZYME(5,1)\|VOLATILE ORGANIC(5,1)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOMATERIAL(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DIFFICULT CHALLENGE(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|FUNCTION VOID SPACE(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|\|(CN102395653)\|HYDROCARBONACEOUS MATERIAL(100,46)\|INFRASTRUCTURE CONSTRUCTION(100,23)\|INFRASTRUCTURE(100,22)\|ENCAPSULATED VOLUME(100,21)\|POSITIVE PRESSURE(100,16)\|CONSTRUCTED PERMEABILITY(100,13)\|RECOVERING HYDROCARBON(100,11)\|ECONOMICALLY COMPETITIVE RECOVERY(74,1)\|UNDERGROUND AQUIFER CONTAMINATION(67,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(63,2)\|DIRTY FINE PARTICULATE(63,1)\|COMPACTED FILL(57,6)\|BENTONITE CLAY(56,1)\|GASEOUS COMPONENT(54,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(52,6)\|IMPOUNDMENT(50,64)\|CLAY LINING(50,1)\|GASEOUS FLUID(49,4)\|CONTROL INFRASTRUCTURE(46,23)\|OXIDIZING GAS(45,1)\|SYNTHETIC CLAY(41,1)\|FLUSH HYDROCARBON VAPOR(38,1)\|DRAINAGE PIPE(37,2)\|ECONOMICS(36,1)\|TEMPERATURE GEOMEMBRANE(36,1)\|GAS OXIDATION(34,2)\|DIFFICULT CHALLENGE(34,1)\|BRINE SOLUTION(32,1)\|CLAY(31,7)\|FLUSHING(31,4)\|SOLVENT RECOVERY(30,2)\|HYDROCARBON RESIDUE(30,1)\|PERMEABILITY CONTROL IMPOUNDMENT(29,3)\|OBSERVABLE(29,1)\|IMPOUNDMENT WALL(28,11)\|REMEDIATION(28,2)\|ASSURANCE(28,1)\|ENVIRONMENTAL HAZARD(28,1)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|SEALANT(28,1)\|PERMEABILITY(27,27)\|HYDROCARBON PRODUCTION(25,13)\|ENCLOSED VOLUME(25,7)\|UNDERGROUND MINING(25,2)\|SEGMENTED CAPSULE IMPOUNDMENT(24,3)\|BRINE(23,1)\|FREEZE WALL(22,3)\|GASEOUS MATERIAL(22,3)\|BLASTING(22,2)\|VOID SPACE(21,6)\|AIR PREVENTING(21,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|LEAK(21,1)\|REFRACTORY CEMENT(20,4)\|BIOMASS(20,3)\|REMOVING HYDROCARBON(20,3)\|HYDROCARBON MATERIAL FLUSHING(20,1)\|OUTPUT CAPACITY(20,1)\|REMOVING PRODUCT(20,1)\|ADDITIVE(18,14)\|STOICHIOMETRIC CONDITION(18,3)\|TOTAL VOLUME(18,2)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(18,1)\|PREVENTABLE WATER BODY(18,1)\|GRAVEL(17,3)\|GROUT(17,3)\|REBAR(17,3)\|ADAPTABLE WATER BODY(16,1)\|SURFACE DISTURBANCE(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|BIOCHEMICALLY OXIDIZE ORE(15,1)\|HEATED HYDROCARBONACEOUS MATERIAL(15,1)\|MINE CAPSULE IMPOUNDMENT(15,1)\|WATER POLLUTION(15,1)\|AFT BERM PERMEABILITY(14,1)\|IMPOUNDMENT CONTAINMENT CAPSULE(14,1)\|LIMIT WATER CONSUMPTION(14,1)\|PROPANE(12,6)\|IMPERMEABLE FLOOR(12,3)\|NEARBY IMPOUNDMENT(12,2)\|TRILLION BARREL(12,2)\|BENTONITE AMENDED SOIL(12,1)\|HYDRO LEAN SHALE(12,1)\|TEXTURED BUILT TAIL BERM(12,1)\|WATER CONSUMPTION(12,1)\|WOVEN BAMBOO BASKET(12,1)\|PEAT(11,4)\|RADIO FREQUENCY(11,3)\|SOIL COMPACTION(11,3)\|IMPERMEABLE SIDEWALL(11,2)\|VOID VOLUME(10,7)\|GUIDELINE(10,4)\|MINED CRUSHED STONE(10,2)\|AVERAGE SIZE(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|COMMINUTED AGGLOMERATE(10,1)\|HEATING(10,1)\|HYDROCARBON LEAN SHALE(10,1)\|IMPOUNDMENT PERIMETER(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|LANDFILL IMPOUNDMENT(10,1)\|LEAK PROOF EXTRACTION IMPOUNDMENT(10,1)\|NANOCARBON FULLERENE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SPRAYED CEMENT SLURRY(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|IMPOUNDMENT HEIGHT(9,2)\|COMPACTED GEOGRID(9,1)\|CONDUIT STRUCTURING(9,1)\|DEBT PAYBACK(9,1)\|ECONOMIC VALUATION(9,1)\|EMPTY IMPOUNDMENT(9,1)\|ENGINEERED CARBON REINFORCED GRID(9,1)\|GASEOUS HYDROCARBON COMBUSTION HEATER(9,1)\|GEOLOGICAL RESERVOIR ANALYSIS(9,1)\|GEOSYNTHETIC FABRICS(9,1)\|GRADE CEMENT SLURRY(9,1)\|HYDROCARBON EXCAVATION(9,1)\|IMPOUNDMENT COLLECTION(9,1)\|IMPOUNDMENT SIDEWALL(9,1)\|INFRASTRUCTURE STABILIZATION(9,1)\|METHANEDIONE RESOLUTION(9,1)\|MINING AVOIDANCE(9,1)\|NEARBY INFRASTRUCTURE(9,1)\|NONCIRCULAR TUBING(9,1)\|PILED RUBBLE(9,1)\|PIT EXCAVATION(9,1)\|REGULATORY FLUID MIGRATION REGULATION(9,1)\|REMAINING SHALE DECREASING WETTABILITY(9,1)\|RESISTANT PVC LINER(9,1)\|THERMALLY DETERIORATED WASTE SHALE(9,1)\|UNCOVERED CAPSULE(9,1)\|UNDERGROUND RUBBLE CHANNEL(9,1)\|UNRECOVERED HYDROCARBON(9,1)\|UNUSED RESOURCE(9,1)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|LIQUID PRODUCT(7,11)\|GASEOUS PRODUCT(7,4)\|CONVECTIVE HEATING(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HORIZONTAL MINING(7,2)\|OIL BLEND(7,2)\|UNCONTROLLED MIGRATION PREVENTION(7,2)\|API MODIFIER(7,1)\|ATMOSPHERIC POLLUTANT(7,1)\|CANADIAN TAR SAND(7,1)\|CARBONATE DECOMPOSITION(7,1)\|CEMENT REINFORCEMENT(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DECREASING HYDROGENATION(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|GEOTEXTILE BAG(7,1)\|GRAVITY ASSISTED DRAIN(7,1)\|GRAVITY DRAINAGE PROFILE(7,1)\|HYDROCARBON ENRICHMENT(7,1)\|HYDROCARBON EXCAVATED VOLUME(7,1)\|HYDROCARBON RICHNESS(7,1)\|HYDROCARBON UNCONTROLLED RELEASE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPERVIOUS BED(7,1)\|IMPOUNDMENT FLOOR(7,1)\|INORGANIC COMPONENT(7,1)\|INSULATION CONTAINMENT(7,1)\|MATERIAL HANDLING COST(7,1)\|MESSY DUMP(7,1)\|MINING HAUL TRUCK(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PLURAL REFERENT(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REGULATORY REGULATION(7,1)\|REINFORCED CEMENT(7,1)\|SHALE MINING(7,1)\|SHELL ICP(7,1)\|SOIL AMENDMENT(7,1)\|SOY INSULATOR(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|USEABLE BODYA GOOD BALANCE(7,1)\|WATERPROOF QUALITY INSULATION(7,1)\|WELLBORE DRILLING(7,1)\|HEAT TRANSFER(6,11)\|HYDROGEN DONOR(6,7)\|COMPACTED FILL TOP(6,3)\|CONVECTION(6,3)\|HEAT PIPE(6,3)\|MINED HYDROCARBONACEOUS MATERIAL(6,3)\|PYROLYSIS(6,3)\|BIOREMEDIATION(6,2)\|GASEOUS LIGHT HYDROCARBON(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|BUILT CAPSULE(6,1)\|CARBON REINFORCING GRID(6,1)\|CERMET COMPOSITE(6,1)\|COLLECTION TROUGH(6,1)\|CONSTRUCTED SULFUR CAPSULE(6,1)\|CONTAINMENT VESSEL SEGMENTATION(6,1)\|CONTAINMENT VESSEL STRUCTURE(6,1)\|DAMAGING STRESS(6,1)\|ECONOMIC FACTOR(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTNESS(6,1)\|ENRICHMENT SENSOR(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|EXTRACTION CAPSULE TREATMENT ZONE(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|FORMATION EXPERIMENTAL MODELING(6,1)\|GEOPOLITICAL FACTOR(6,1)\|HYDROCARBON BEARING(6,1)\|HYDROCARBONACEOUS MATERIAL RESULT(6,1)\|IMMEDIATE INTRODUCTION(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT LIFE SPAN(6,1)\|IMPOUNDMENT REGION(6,1)\|LEACHATE PRODUCTION(6,1)\|LEAK PROOF CONTAINMENT VESSEL(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MAXIMIZE RECOVERY(6,1)\|METHANEDIONE PRODUCTION(6,1)\|MICROBIAL STRAIN(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|OUTER CAPSULE IMPOUNDMENT(6,1)\|PERFORATED HEATING PIPE(6,1)\|PERMEABILITY BARRIER(6,1)\|PERMEABLE PARTICLE(6,1)\|PIPE CONDENSER(6,1)\|PIPE PERFORATION(6,1)\|PREFABRICATED PIECE(6,1)\|PREFORMED PIECE(6,1)\|PROVEN RESERVOIR(6,1)\|RECOVERY STEAM(6,1)\|REDUCING CO2EMISSIONS(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|RESISTIVE HEATER(6,1)\|REUSABLE PIPE(6,1)\|ROTARY RETORT(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STAGED CONTAINMENT VESSEL(6,1)\|STAGING PIPE(6,1)\|SUBTERRANEAN TREATMENT ZONE(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SUPPORTIVE IMPOUNDMENT WALL FORMATION(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANOCARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|TUNNELING(6,1)\|ULTRASONIC GENERATOR(6,1)\|VOLATILE HYDROCARBON(6,1)\|MINED MATERIAL(5,5)\|ENZYME(5,4)\|HEATING RATE(5,4)\|AGITATION(5,3)\|ADJACENT IMPOUNDMENT(5,2)\|ANCHOR MEMBER(5,2)\|ASPHALTENE(5,2)\|CATHETER(5,2)\|COMBUSTION EXHAUST GAS(5,2)\|CRUSHING(5,2)\|CULLET(5,2)\|DETONATION(5,2)\|EXPLOSION(5,2)\|FIBERGLASS(5,2)\|HYDROCARBON LIQUID(5,2)\|HYDROGEN CONTENT(5,2)\|INVESTIGATION(5,2)\|PORTABLE COMBUSTION CHAMBER(5,2)\|PRECIPITATION(5,2)\|RECIRCULATION(5,2)\|SEQUESTRATION(5,2)\|SWELLING(5,2)\|ABUNDANT LIGHT HYDROCARBON(5,1)\|AMBIENT ENVIRONMENT(5,1)\|ANAEROBIC CONDITION(5,1)\|BARRIER MANUFACTURE(5,1)\|BLENDING KEROGEN OIL(5,1)\|CAPACITY INDICATOR(5,1)\|CENTRAL GATHERING PIPE(5,1)\|CHROMATOGRAPHIC LOCATION(5,1)\|COMPLEX MACHINERY(5,1)\|COMPUTER AIDED MINING(5,1)\|COMPUTER EQUIPMENT(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|CONSTRUCTED SULFUR CONTAINMENT VESSEL(5,1)\|CONTAINMENT DISPOSAL AREA(5,1)\|CONTAINMENT VOLUME(5,1)\|COOLING INCREASE(5,1)\|CRUDE EXTRACTION(5,1)\|DECREASING SULFUR(5,1)\|DECREASING VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|ENCAPSULATED IMPOUNDMENT AREA(5,1)\|ENRICHED OIL BEARING ORE(5,1)\|EXPOSED UNDISTURBED GROUND(5,1)\|EXTRACTION PORT(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLOOR CONSTRUCTION(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GEOLOGICAL LOCATION(5,1)\|HORIZONTAL BOREHOLE(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBON VAPOR(5,1)\|HYDROCARBONACEOUS MATERIAL BIOHYDROXYLATION(5,1)\|INFRASTRUCTURE LOCATION(5,1)\|INORGANIC MATTER(5,1)\|ION RESIN EXCHANGE(5,1)\|KEROGEN REMOVAL(5,1)\|LARGE CONTAINMENT IMPOUNDMENT(5,1)\|LAYER COMPACTION(5,1)\|LOCALIZED HEATING ZONE(5,1)\|METEOROLOGICAL DATA FACTOR(5,1)\|MINIMAL WASTE(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONHYDROCARBON(5,1)\|NONOXIDIZING GAS(5,1)\|OIL SHALE ORE(5,1)\|OPEN ENDED CAPSULE IMPOUNDMENT(5,1)\|OPTIMIZATION REASON(5,1)\|PATHWAY(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PREVENT ACCIDENTAL LEACHING(5,1)\|PREVENTION MEASURE(5,1)\|PUMPING PIPE(5,1)\|PURGE GAS(5,1)\|RECOVERING OIL(5,1)\|RECUPERATOR(5,1)\|REFORMATION(5,1)\|RELEVANT MEASUREMENT(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RETURN DILUENT(5,1)\|ROUND TUBING(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|SPRAYED LIQUID EMULSION(5,1)\|STAGED PROCESSING(5,1)\|STEEL RETORT(5,1)\|STRUCTURED FEATURE(5,1)\|SUPPLEMENTAL HEATING(5,1)\|SUPPORTING BERM(5,1)\|TECHNICAL CHALLENGE(5,1)\|TRANSFER DEFLATION(5,1)\|TRANSPORT CONDUIT(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNDERGROUND AQUIFER(5,1)\|UPGRADING(5,1)\|VOLATILE ORGANIC(5,1)\|WATERTIGHT COVER(5,1)\|HEATED FLUID(4,3)\|INJECTION RATE(4,3)\|SILO(4,3)\|VAPOR PRODUCTION(4,2)\|ACROSS MULTIPLE IMPOUNDMENT(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADVENT(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALONE MEET(3,1)\|ANCHOR PILE STRUCTURE(3,1)\|AQUEOUS MUD CONDITION(3,1)\|AROMATICS(3,1)\|ASSAYING(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOGLASS(3,1)\|BIOLEACHING(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CATALYTIC GAS(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|CENTRAL RESERVOIR(3,1)\|COAL COMBINATION(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONCENTRATE(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED GEOMEMBRANE LAYER(3,1)\|CONTAINMENT CONSTRUCTION(3,1)\|CONTAINMENT VESSEL CONSTRUCTION(3,1)\|CONTOUR(3,1)\|CONTROLLED QUALITY SHALE(3,1)\|COOLING FLUID(3,1)\|COOLING PIPE(3,1)\|CURRENCY(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DEADMAN(3,1)\|DOWNWARDLY TRANSFERRED LIQUID(3,1)\|DUMPING(3,1)\|EARTH FORMATION(3,1)\|ELECTRICITY(3,1)\|ELECTROLYTE(3,1)\|ELECTROPLATING(3,1)\|ELEVATOR(3,1)\|ENHANCE REMOVAL(3,1)\|ENHANCER(3,1)\|ESTIMATE SOURCE(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLEXIBLE HOUSING(3,1)\|FLOTATION(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID EXTRACTION(3,1)\|FRACTURE(3,1)\|FRACTURING(3,1)\|FUNCTIONAL VOID SPACE(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS COMBUSTION(3,1)\|GAS GATHERING(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GAS RELEASE(3,1)\|GEOSYNTHETIC MEMBRANE(3,1)\|GRADE PLANE(3,1)\|HALF ACRE(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HAULING(3,1)\|HEAT ABSORPTION(3,1)\|HEATING CONDUIT COST(3,1)\|HEATING CONDUIT LOCATION(3,1)\|HEATING FLUID ISOLATION(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTRATION(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBONACEOUS MATERIAL COMPACTION(3,1)\|HYDROTREAT(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE BOTTOM(3,1)\|\|(CN102395653)\|HYDROCARBONACEOUS MATERIAL(100,46)\|INFRASTRUCTURE CONSTRUCTION(100,23)\|INFRASTRUCTURE(100,21)\|POSITIVE PRESSURE(100,15)\|CONSTRUCTED PERMEABILITY(100,12)\|RECOVERING HYDROCARBON(100,11)\|ENCAPSULATED VOLUME(94,19)\|ECONOMICALLY COMPETITIVE RECOVERY(84,1)\|UNDERGROUND AQUIFER CONTAMINATION(75,1)\|DIRTY FINE PARTICULATE(71,1)\|GASEOUS FLUID(70,5)\|BENTONITE CLAY(64,1)\|GASEOUS COMPONENT(61,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(58,6)\|CLAY LINING(56,1)\|IMPOUNDMENT(46,63)\|SYNTHETIC CLAY(46,1)\|FLUSH HYDROCARBON VAPOR(43,1)\|DRAINAGE PIPE(42,2)\|CONTROL INFRASTRUCTURE(41,21)\|ECONOMICS(40,1)\|TEMPERATURE GEOMEMBRANE(40,1)\|UNDESIRED HYDROCARBON(40,1)\|DIFFICULT CHALLENGE(39,1)\|BRINE SOLUTION(36,1)\|HYDROCARBON RESIDUE(34,1)\|SOLVENT RECOVERY(33,2)\|OBSERVABLE(33,1)\|IMPOUNDMENT WALL(32,11)\|PERMEABILITY CONTROL IMPOUNDMENT(32,3)\|ASSURANCE(32,1)\|ENVIRONMENTAL HAZARD(32,1)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(32,1)\|SEALANT(32,1)\|REMEDIATION(31,2)\|ENCLOSED VOLUME(29,7)\|UNDERGROUND MINING(28,2)\|SEGMENTED CAPSULE IMPOUNDMENT(27,3)\|BRINE(26,1)\|VOID SPACE(25,5)\|FREEZE WALL(25,3)\|GASEOUS MATERIAL(25,3)\|BLASTING(25,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(24,1)\|LEAK(24,1)\|HYDROCARBON MATERIAL FLUSHING(23,1)\|OUTPUT CAPACITY(23,1)\|REMOVING PRODUCT(23,1)\|REFRACTORY CEMENT(22,4)\|BIOMASS(22,3)\|REMOVING HYDROCARBON(22,3)\|ADDITIVE(20,14)\|GRAVEL(20,3)\|REBAR(20,3)\|STOICHIOMETRIC CONDITION(20,3)\|TOTAL VOLUME(20,2)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(20,1)\|PREVENTABLE WATER BODY(20,1)\|GROUT(19,3)\|ADAPTABLE WATER BODY(18,1)\|SURFACE DISTURBANCE(18,1)\|UNDERGROUND FRESHWATER AQUIFER(18,1)\|LIGNITE(17,4)\|BIOCHEMICALLY OXIDIZE ORE(17,1)\|HEATED HYDROCARBONACEOUS MATERIAL(17,1)\|MINE CAPSULE IMPOUNDMENT(17,1)\|WATER POLLUTION(17,1)\|AFT BERM PERMEABILITY(16,1)\|IMPOUNDMENT CONTAINMENT CAPSULE(16,1)\|LIMIT WATER CONSUMPTION(16,1)\|HYDROCARBON PRODUCTION(15,12)\|IMPERMEABLE FLOOR(14,3)\|NEARBY IMPOUNDMENT(14,2)\|TRILLION BARREL(14,2)\|BENTONITE AMENDED SOIL(14,1)\|HYDRO LEAN SHALE(14,1)\|WATER CONSUMPTION(14,1)\|WOVEN BAMBOO BASKET(14,1)\|PROPANE(13,6)\|PEAT(13,4)\|RADIO FREQUENCY(13,3)\|IMPERMEABLE SIDEWALL(13,2)\|VOID VOLUME(12,7)\|SOIL COMPACTION(12,3)\|MINED CRUSHED STONE(12,2)\|GUIDELINE(11,4)\|AVERAGE SIZE(11,1)\|BIOEXTRACTION SCENARIO(11,1)\|CHALLENGING ENDEAVOR(11,1)\|COLLECTIVE IMPOUNDMENT(11,1)\|COMMINUTED AGGLOMERATE(11,1)\|HEATING(11,1)\|HYDROCARBON LEAN SHALE(11,1)\|IMPOUNDMENT PERIMETER(11,1)\|INFRASTRUCTURE SHUTDOWN(11,1)\|LANDFILL IMPOUNDMENT(11,1)\|LEAK PROOF EXTRACTION IMPOUNDMENT(11,1)\|NANOCARBON FULLERENE(11,1)\|SEWAGE IMPOUNDMENT(11,1)\|SPRAYED CEMENT SLURRY(11,1)\|SUBDIVIDED IMPOUNDMENT(11,1)\|WATERPROOF QUALITY ENGINEERING(11,1)\|UNDISTURBED GEOLOGICAL FORMATION(10,3)\|IMPOUNDMENT HEIGHT(10,2)\|COMPACTED GEOGRID(10,1)\|CONDUIT STRUCTURING(10,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(10,1)\|DEBT PAYBACK(10,1)\|ECONOMIC VALUATION(10,1)\|EMPTY IMPOUNDMENT(10,1)\|ENGINEERED CARBON REINFORCED GRID(10,1)\|GASEOUS HYDROCARBON COMBUSTION HEATER(10,1)\|GEOLOGICAL RESERVOIR ANALYSIS(10,1)\|GEOSYNTHETIC FABRICS(10,1)\|GRADE CEMENT SLURRY(10,1)\|HYDROCARBON EXCAVATION(10,1)\|IMPOUNDMENT COLLECTION(10,1)\|IMPOUNDMENT SIDEWALL(10,1)\|INFRASTRUCTURE STABILIZATION(10,1)\|METHANEDIONE RESOLUTION(10,1)\|MINING AVOIDANCE(10,1)\|NEARBY INFRASTRUCTURE(10,1)\|NONCIRCULAR TUBING(10,1)\|PILED RUBBLE(10,1)\|PIT EXCAVATION(10,1)\|REGULATORY FLUID MIGRATION REGULATION(10,1)\|REMAINING SHALE DECREASING WETTABILITY(10,1)\|RESISTANT PVC LINER(10,1)\|TEXTURED BUILT TAIL(10,1)\|THERMALLY DETERIORATED WASTE SHALE(10,1)\|UNCOVERED CAPSULE(10,1)\|UNDERGROUND RUBBLE CHANNEL(10,1)\|UNRECOVERED HYDROCARBON(10,1)\|UNUSED RESOURCE(10,1)\|LIQUID PRODUCT(8,11)\|GASEOUS PRODUCT(8,4)\|CONVECTIVE HEATING(8,2)\|HORIZONTAL MINING(8,2)\|OIL BLEND(8,2)\|UNCONTROLLED MIGRATION PREVENTION(8,2)\|API MODIFIER(8,1)\|ATMOSPHERIC POLLUTANT(8,1)\|CANADIAN TAR SAND(8,1)\|CARBONATE DECOMPOSITION(8,1)\|CEMENT REINFORCEMENT(8,1)\|CONTAINMENT BOUNDARY(8,1)\|CRANE SUSPENDED EXCAVATOR(8,1)\|CRUSHED ORE(8,1)\|DECREASING HYDROGENATION(8,1)\|ECONOMIC OPPORTUNITY(8,1)\|EXCAVATED CAVITY(8,1)\|GEOTEXTILE BAG(8,1)\|GRAVITY ASSISTED DRAIN(8,1)\|GRAVITY DRAINAGE PROFILE(8,1)\|HYDROCARBON ENRICHMENT(8,1)\|HYDROCARBON EXCAVATED VOLUME(8,1)\|HYDROCARBON RICHNESS(8,1)\|HYDROCARBON UNCONTROLLED RELEASE(8,1)\|IMPERMEABLE BARRIER ZONE(8,1)\|IMPERVIOUS BED(8,1)\|IMPOUNDMENT FLOOR(8,1)\|INORGANIC COMPONENT(8,1)\|INSULATION CONTAINMENT(8,1)\|MATERIAL HANDLING COST(8,1)\|MESSY DUMP(8,1)\|MINING HAUL TRUCK(8,1)\|NATIVE BACTERIA(8,1)\|NATURAL DISTRIBUTED COMBUSTOR(8,1)\|ORE SOLVENT EXTRACTION(8,1)\|PILLAR MINING(8,1)\|PLURAL REFERENT(8,1)\|REFORMING CATALYST(8,1)\|REFORMING ZONE(8,1)\|REGULATORY REGULATION(8,1)\|REINFORCED CEMENT(8,1)\|SHALE MINING(8,1)\|SHELL ICP(8,1)\|SOIL AMENDMENT(8,1)\|SOY INSULATOR(8,1)\|STOICHIOMETRIC COMBUSTION(8,1)\|SUPER DISPOSITION(8,1)\|TAR SAND BITUMEN TREATMENT(8,1)\|WATERPROOF QUALITY INSULATION(8,1)\|WELLBORE DRILLING(8,1)\|HEAT TRANSFER(7,11)\|HYDROGEN DONOR(7,7)\|CONVECTION(7,3)\|HEAT PIPE(7,3)\|MINED HYDROCARBONACEOUS MATERIAL(7,3)\|PYROLYSIS(7,3)\|BIOREMEDIATION(7,2)\|GASEOUS LIGHT HYDROCARBON(7,2)\|ACCEPTED PIPELINE STANDARD(7,1)\|BUILT CAPSULE(7,1)\|CARBON REINFORCING GRID(7,1)\|CERMET COMPOSITE(7,1)\|COLLECTION TROUGH(7,1)\|CONSTRUCTED SULFUR CAPSULE(7,1)\|CONTAINMENT VESSEL SEGMENTATION(7,1)\|CONTAINMENT VESSEL STRUCTURE(7,1)\|DAMAGING STRESS(7,1)\|ECONOMIC FACTOR(7,1)\|EMBEDDED CONDUIT(7,1)\|ENHANCE COMPACTNESS(7,1)\|ENRICHMENT SENSOR(7,1)\|EXPLICITLY RECITED LIMIT(7,1)\|EXTRACTION CAPSULE TREATMENT ZONE(7,1)\|FLOOR LEVELING(7,1)\|FLUSH HYDROCARBON(7,1)\|FORMATION EXPERIMENTAL MODELING(7,1)\|GEOPOLITICAL FACTOR(7,1)\|HYDROCARBON BEARING(7,1)\|HYDROCARBONACEOUS MATERIAL RESULT(7,1)\|IMMEDIATE INTRODUCTION(7,1)\|IMPOUNDMENT DEPTH(7,1)\|IMPOUNDMENT LIFE SPAN(7,1)\|IMPOUNDMENT REGION(7,1)\|LEACHATE PRODUCTION(7,1)\|LEAK PROOF CONTAINMENT VESSEL(7,1)\|LOCALIZED HOTSPOT ELIMINATION(7,1)\|MAXIMIZE RECOVERY(7,1)\|METHANEDIONE PRODUCTION(7,1)\|MICROBIAL STRAIN(7,1)\|MINERAL LINER(7,1)\|MINING ORE GRADE(7,1)\|MOISTURE MIGRATION(7,1)\|ORE MOISTURE CONTENT(7,1)\|OUTER CAPSULE IMPOUNDMENT(7,1)\|PERFORATED HEATING PIPE(7,1)\|PERMEABILITY BARRIER(7,1)\|PERMEABLE PARTICLE(7,1)\|PIPE CONDENSER(7,1)\|PIPE PERFORATION(7,1)\|PREFABRICATED PIECE(7,1)\|PREFORMED PIECE(7,1)\|PROVEN RESERVOIR(7,1)\|RECOVERY STEAM(7,1)\|REDUCING CO2EMISSIONS(7,1)\|REFRACTORY CEMENT PIPE(7,1)\|RESISTIVE HEATER(7,1)\|REUSABLE PIPE(7,1)\|ROTARY RETORT(7,1)\|SPENT SHALE SOLID RINSING(7,1)\|STAGED CONTAINMENT VESSEL(7,1)\|STAGING PIPE(7,1)\|SUBTERRANEAN TREATMENT ZONE(7,1)\|SUPPLEMENTAL FUEL(7,1)\|SUPPORTIVE IMPOUNDMENT WALL FORMATION(7,1)\|SYNTHETIC GEOGRID(7,1)\|SYNTHETIC NANOCARBON(7,1)\|TAR SAND DEPOSIT(7,1)\|TOXIC EFFLUENT(7,1)\|TUNNELING(7,1)\|ULTRASONIC GENERATOR(7,1)\|VOLATILE HYDROCARBON(7,1)\|CLAY(6,5)\|MINED MATERIAL(6,5)\|ENZYME(6,4)\|AGITATION(6,3)\|ADJACENT IMPOUNDMENT(6,2)\|ANCHOR MEMBER(6,2)\|ASPHALTENE(6,2)\|CATHETER(6,2)\|COMBUSTION EXHAUST GAS(6,2)\|COMPACTED FILL TOP(6,2)\|CRUSHING(6,2)\|CULLET(6,2)\|DETONATION(6,2)\|EXPLOSION(6,2)\|FIBERGLASS(6,2)\|HYDROCARBON LIQUID(6,2)\|HYDROGEN CONTENT(6,2)\|INVESTIGATION(6,2)\|PORTABLE COMBUSTION CHAMBER(6,2)\|PRECIPITATION(6,2)\|RECIRCULATION(6,2)\|SEQUESTRATION(6,2)\|SWELLING(6,2)\|HEATING RATE(5,4)\|HEATED FLUID(5,3)\|INJECTION RATE(5,3)\|SILO(5,3)\|VAPOR PRODUCTION(5,2)\|ABUNDANT LIGHT HYDROCARBON(5,1)\|AMBIENT ENVIRONMENT(5,1)\|ANAEROBIC CONDITION(5,1)\|BARRIER MANUFACTURE(5,1)\|BLENDING KEROGEN OIL(5,1)\|CAPACITY INDICATOR(5,1)\|CENTRAL GATHERING PIPE(5,1)\|CHROMATOGRAPHIC LOCATION(5,1)\|COMPLEX MACHINERY(5,1)\|COMPUTER AIDED MINING(5,1)\|COMPUTER EQUIPMENT(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|CONSTRUCTED SULFUR CONTAINMENT VESSEL(5,1)\|CONTAINMENT DISPOSAL AREA(5,1)\|CONTAINMENT VOLUME(5,1)\|COOLING INCREASE(5,1)\|CRUDE EXTRACTION(5,1)\|DECREASING SULFUR(5,1)\|DECREASING VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|ENCAPSULATED IMPOUNDMENT AREA(5,1)\|ENRICHED OIL BEARING ORE(5,1)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(5,1)\|EXPOSED UNDISTURBED GROUND(5,1)\|EXTRACTION PORT(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLOOR CONSTRUCTION(5,1)\|GAS OXIDATION(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GEOLOGICAL LOCATION(5,1)\|HORIZONTAL BOREHOLE(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBON VAPOR(5,1)\|HYDROCARBONACEOUS MATERIAL BIOHYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|INFRASTRUCTURE LOCATION(5,1)\|INORGANIC MATTER(5,1)\|ION RESIN EXCHANGE(5,1)\|KEROGEN REMOVAL(5,1)\|LARGE CONTAINMENT IMPOUNDMENT(5,1)\|LAYER COMPACTION(5,1)\|LOCALIZED HEATING ZONE(5,1)\|METEOROLOGICAL DATA FACTOR(5,1)\|MINIMAL WASTE(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONHYDROCARBON(5,1)\|NONOXIDIZING GAS(5,1)\|OIL SHALE ORE(5,1)\|OPEN ENDED CAPSULE IMPOUNDMENT(5,1)\|OPTIMIZATION REASON(5,1)\|PATHWAY(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PREVENT ACCIDENTAL LEACHING(5,1)\|PREVENTION MEASURE(5,1)\|PROBLEMSAND(5,1)\|PUMPING PIPE(5,1)\|PURGE GAS(5,1)\|RECOVERING OIL(5,1)\|RECUPERATOR(5,1)\|REFORMATION(5,1)\|RELEVANT MEASUREMENT(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RETURN DILUENT(5,1)\|ROUND TUBING(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|SPRAYED LIQUID EMULSION(5,1)\|STAGED PROCESSING(5,1)\|STEEL RETORT(5,1)\|STRUCTURED FEATURE(5,1)\|SUPPLEMENTAL HEATING(5,1)\|SUPPORTING BERMS(5,1)\|TECHNICAL CHALLENGE(5,1)\|TRANSFER DEFLATION(5,1)\|TRANSPORT CONDUIT(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNDERGROUND AQUIFER(5,1)\|UPGRADING(5,1)\|VOLATILE ORGANIC(5,1)\|WATERTIGHT COVER(5,1)\|ACROSS MULTIPLE IMPOUNDMENT(4,1)\|ADJACENT INFRASTRUCTURE(4,1)\|ADVENT(4,1)\|AGGREGATE PRODUCTION(4,1)\|ALONE MEET(4,1)\|ANCHOR PILE STRUCTURE(4,1)\|AQUEOUS MUD CONDITION(4,1)\|AROMATICS(4,1)\|ASSAYING(4,1)\|AVAILABLE ADDRESSING(4,1)\|BAUXITE(4,1)\|BINDER(4,1)\|BIOCATALYST(4,1)\|BIOGLASS(4,1)\|BIOLEACHING(4,1)\|BITUMEN SOURCE(4,1)\|CALCINED PETROLEUM COKE(4,1)\|CATALYTIC GAS(4,1)\|CATALYTICALLY ACTIVE METAL(4,1)\|CENTRAL RESERVOIR(4,1)\|COAL COMBINATION(4,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(4,1)\|COMPOSITE WALL(4,1)\|COMPOUND SUBSTITUTION(4,1)\|CONCENTRATE(4,1)\|CONDENSABILITY(4,1)\|CONDUIT PASS(4,1)\|CONDUIT WALL(4,1)\|CONSTRUCTED GEOMEMBRANE LAYER(4,1)\|CONTAINMENT CONSTRUCTION(4,1)\|CONTAINMENT VESSEL CONSTRUCTION(4,1)\|CONTOUR(4,1)\|CONTROLLED QUALITY SHALE(4,1)\|COOLING FLUID(4,1)\|COOLING PIPE(4,1)\|CURRENCY(4,1)\|CYCLOHEXANE(4,1)\|CYCLOPENTANE(4,1)\|DEADMAN(4,1)\|DICTATION(4,1)\|DOWNWARDLY TRANSFERRED LIQUID(4,1)\|DUMPING(4,1)\|EARTH FORMATION(4,1)\|ELECTRICITY(4,1)\|ELECTROLYTE(4,1)\|ELECTROPLATING(4,1)\|ELEVATOR(4,1)\|ENHANCE REMOVAL(4,1)\|ENHANCER(4,1)\|ESTIMATE SOURCE(4,1)\|EXCAVATION AREA(4,1)\|FINAL HYDROCARBON PRODUCT(4,1)\|FINAL PRODUCT RECOVERY(4,1)\|FINE MESH(4,1)\|FLEXIBLE HOUSING(4,1)\|FLOTATION(4,1)\|FLUID COMMUNICATION(4,1)\|FLUID EXTRACTION(4,1)\|FRACTURE(4,1)\|FRACTURING(4,1)\|FUNCTIONAL VOID SPACE(4,1)\|GAS BARRIER(4,1)\|GAS COLLECTION OUTLET(4,1)\|GAS COMBUSTION(4,1)\|GAS GATHERING(4,1)\|GAS INJECTION(4,1)\|GAS MIGRATION(4,1)\|GAS RELEASE(4,1)\|GEOSYNTHETIC MEMBRANE(4,1)\|GRADE PLANE(4,1)\|HALF ACRE(4,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(4,1)\|HAULING(4,1)\|HEAT ABSORPTION(4,1)\|HEATING CONDUIT COST(4,1)\|HEATING CONDUIT LOCATION(4,1)\|HEATING FLUID ISOLATION(4,1)\|HOLDING TANK PROXIMITY(4,1)\|HOT GAS FILTRATION(4,1)\|HYDROCARBON GAS(4,1)\|HYDROCARBONACEOUS MATERIAL COMPACTION(4,1)\|HYDROTREAT(4,1)\|\|(AU2010213774)\|HYDROCARBONACEOUS MATERIAL(100,45)\|INFRASTRUCTURE(100,23)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,17)\|CONSTRUCTED PERMEABILITY(100,13)\|RECOVERING HYDROCARBON(100,13)\|ENCAPSULATED VOLUME(93,29)\|GASEOUS FLUID(52,6)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(48,6)\|GASEOUS COMPONENT(39,4)\|CONTROL INFRASTRUCTURE(37,25)\|FLUSH RESIDUAL HYDROCARBON(37,1)\|FLUSH HYDROCARBON VAPOR(36,1)\|COLLECTING REMOVED HYDROCARBON(27,2)\|HYDROCARBON COMBUSTION(26,2)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(26,1)\|PERMEABILITY CONTROL IMPOUNDMENT(25,4)\|HYDROCARBONACEOUS MATERIAL FLUSHING(25,1)\|GASEOUS MATERIAL(20,3)\|HEATED HYDROCARBONACEOUS MATERIAL(20,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(20,1)\|VOID SPACE(19,5)\|MALFUNCTION(19,1)\|SECTIONED CAPSULE IMPOUNDMENT(18,2)\|STOICHIOMETRIC CONDITION(18,2)\|COMPACTED FILL CEILING(16,3)\|TOTAL VOLUME(16,2)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(16,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(15,1)\|UNDERGROUND FRESHWATER AQUIFER(15,1)\|LIGNITE(14,4)\|QUARRY CAPSULE IMPOUNDMENT(14,1)\|UNCAPPED CAPSULE IMPOUNDMENT(14,1)\|UNDERGROUND RUBBLE CHIMNEY(14,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(13,1)\|NANOCARBON FULLERENE ADDITIVE(13,1)\|STRUCTURED IMPOUNDMENT CAPSULE(13,1)\|HYDROCARBON PRODUCTION(12,11)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|PROPANE(11,6)\|CONTAINMENT CAPSULE(11,2)\|NEARBY IMPOUNDMENT(11,2)\|TAILING BERM(11,2)\|UNRECOVERED HYDROCARBON(11,2)\|COAL(10,7)\|PEAT(10,4)\|BENTONITE CLAY(10,2)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|ENGINEERED PERMEABILITY BARRIER(10,1)\|HYDROCARBON UNCONTROLLED EGRESS(10,1)\|UNDERGROUND MINED HYDROCARBON(10,1)\|BENCH MINING ELEVATION(9,1)\|BIOEXTRACTION SCENARIO(9,1)\|CHALLENGING ENDEAVOR(9,1)\|COLLECTIVE IMPOUNDMENT(9,1)\|EXTERIOR CAPSULE IMPOUNDMENT(9,1)\|GARBAGE IMPOUNDMENT(9,1)\|GRAVITY ASSISTED DRAINAGE PIPE(9,1)\|GRAVITY DRAINAGE ASSISTANCE(9,1)\|INDISCRIMINATE DUMPING(9,1)\|INFRASTRUCTURE SHUTDOWN(9,1)\|MANIPULATED GRADE SHALE(9,1)\|MEDIAN SIZE(9,1)\|SEWAGE IMPOUNDMENT(9,1)\|SUBDIVIDED IMPOUNDMENT(9,1)\|UNTAPPED RESOURCE(9,1)\|WATERPROOF QUALITY ENGINEERING(9,1)\|HEAT PIPE(8,6)\|GUIDELINE(8,3)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CONSTRUCTED SULFUR CAPSULE(8,2)\|IMPOUNDMENT HEIGHT(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MILLING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|VOID VOLUME(7,4)\|CORE DRILLING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|LEAN SHALE(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|LIQUID PRODUCT(6,10)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|CONVECTIVE HEATING(6,2)\|CRUSHED GLASS(6,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(6,2)\|HEATED CONDUIT(6,2)\|HEATING(6,2)\|HORIZONTAL MINING(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|CARBONATE DECOMPOSITION(6,1)\|CO2 EMISSION(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|HYDROGEN DONOR(5,6)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|ANTHEM DEGREE(5,2)\|BLASTING(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|FLOOR CONSTRUCTION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|KEROGEN OIL(4,4)\|HEATED FLUID(4,3)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|PIPING(4,3)\|ANAEROBIC CONDITION(4,1)\|AQUEOUS SLURRY(4,1)\|BARRIER MANUFACTURE(4,1)\|CAPACITY INDICATOR(4,1)\|CAPSULE IMPOUNDMENT AREA(4,1)\|CATALYZING GAS(4,1)\|CEILING CAP(4,1)\|CLAY PIPE(4,1)\|COMMINUTED MASS(4,1)\|COMPOSITION ADMIXTURE(4,1)\|CONCRETE PANEL(4,1)\|CONDUCTIVE CEMENT(4,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(4,1)\|CONSTRUCTED IMPOUNDMENT(4,1)\|DECREASED VISCOSITY(4,1)\|DISPERSION FLUID SENSOR(4,1)\|DUST PARTICLE(4,1)\|ECONOMICALLY VIABLE SOURCE(4,1)\|FAST RECOVERY(4,1)\|FINE COLLECTION(4,1)\|FLUID DRAINAGE(4,1)\|FLUSHING GAS(4,1)\|GAS COMBUSTION HEATER(4,1)\|GASEOUS HYDROCARBON PRODUCT(4,1)\|GEO MEMBRANE LAYER(4,1)\|GEO SYNTHETIC MEMBRANE(4,1)\|GEOLOGICAL LOCATION(4,1)\|HEATING CONDUIT PLACEMENT(4,1)\|HOTSPOT LOCALIZATION(4,1)\|HYDROCARBON VAPOR(4,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(4,1)\|HYDRODESULFURIZATION(4,1)\|IMPOUNDMENT USEFUL LIFE(4,1)\|INORGANIC MATTER(4,1)\|KEROGEN REMOVAL(4,1)\|LAYER COMPACTION(4,1)\|MICROBIOLOGY(4,1)\|MINIMAL WASTE(4,1)\|MINING HAUL TRUCK NEED(4,1)\|MOLTEN CARBONATE FUEL CELL(4,1)\|MONITORING HEAT(4,1)\|NONHEATED BUFFER ZONE(4,1)\|NONOXIDIZING GAS(4,1)\|OIL BLEND(4,1)\|OPTIMIZATION REASON(4,1)\|PIPELINE EXTENSION(4,1)\|PLANT FIBER CELLULOSE(4,1)\|POLYMERIC RESIN(4,1)\|PRECAST PIECE(4,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(4,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(4,1)\|QUALITY DETERIORATION(4,1)\|RECOVERED HYDROCARBON LIQUID(4,1)\|RECOVERING OIL(4,1)\|REFORMATION(4,1)\|RESIDUAL HYDROCARBON PRODUCT(4,1)\|RESIDUAL SHALE REDUCED WETTING(4,1)\|RICH OIL BEARING ORE(4,1)\|ROTATING RETORT(4,1)\|SAND PARTICLE(4,1)\|SEQUENTIAL SOLUTION RECOVERY(4,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(4,1)\|SOLVENT SUBSTITUTED COMPOUND(4,1)\|STAGED PROCESSING(4,1)\|STEAM INJECTION(4,1)\|TECHNICAL CHALLENGE(4,1)\|TREMENDOUS VOLUME(4,1)\|UNCONTROLLED ESCAPE PREVENTION(4,1)\|UNCONTROLLED MIGRATION PREVENTION(4,1)\|VAPOROUS COMPONENT(4,1)\|VARIED ENZYME(4,1)\|VOLATILE ORGANIC(4,1)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOLEACHING(3,1)\|BIOMATERIAL(3,1)\|BIOOXIDATION(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ECONOMICS(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|EXCLUSION(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCLUSION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|LAYER CONDUIT(3,1)\|LAYING WIRE(3,1)\|LIGHTER(3,1)\|LIMITED COMBUSTION INTENT(3,1)\|LIQUID CONDENSATION(3,1)\|LIQUID EMULSION(3,1)\|LUBRICANT COOLANT(3,1)\|\|(AU2010213774)\|HYDROCARBONACEOUS MATERIAL(100,45)\|INFRASTRUCTURE(100,23)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,17)\|CONSTRUCTED PERMEABILITY(100,13)\|RECOVERING HYDROCARBON(100,13)\|ENCAPSULATED VOLUME(93,29)\|GASEOUS FLUID(52,6)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(48,6)\|GASEOUS COMPONENT(39,4)\|CONTROL INFRASTRUCTURE(37,25)\|FLUSH RESIDUAL HYDROCARBON(37,1)\|FLUSH HYDROCARBON VAPOR(36,1)\|COLLECTING REMOVED HYDROCARBON(27,2)\|HYDROCARBON COMBUSTION(26,2)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(26,1)\|PERMEABILITY CONTROL IMPOUNDMENT(25,4)\|HYDROCARBONACEOUS MATERIAL FLUSHING(25,1)\|GASEOUS MATERIAL(20,3)\|HEATED HYDROCARBONACEOUS MATERIAL(20,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(20,1)\|VOID SPACE(19,5)\|MALFUNCTION(19,1)\|SECTIONED CAPSULE IMPOUNDMENT(18,2)\|STOICHIOMETRIC CONDITION(18,2)\|COMPACTED FILL CEILING(16,3)\|TOTAL VOLUME(16,2)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(16,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(15,1)\|UNDERGROUND FRESHWATER AQUIFER(15,1)\|LIGNITE(14,4)\|QUARRY CAPSULE IMPOUNDMENT(14,1)\|UNCAPPED CAPSULE IMPOUNDMENT(14,1)\|UNDERGROUND RUBBLE CHIMNEY(14,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(13,1)\|NANOCARBON FULLERENE ADDITIVE(13,1)\|STRUCTURED IMPOUNDMENT CAPSULE(13,1)\|HYDROCARBON PRODUCTION(12,11)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|PROPANE(11,6)\|CONTAINMENT CAPSULE(11,2)\|NEARBY IMPOUNDMENT(11,2)\|TAILING BERM(11,2)\|UNRECOVERED HYDROCARBON(11,2)\|COAL(10,7)\|PEAT(10,4)\|BENTONITE CLAY(10,2)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|ENGINEERED PERMEABILITY BARRIER(10,1)\|HYDROCARBON UNCONTROLLED EGRESS(10,1)\|UNDERGROUND MINED HYDROCARBON(10,1)\|BENCH MINING ELEVATION(9,1)\|BIOEXTRACTION SCENARIO(9,1)\|CHALLENGING ENDEAVOR(9,1)\|COLLECTIVE IMPOUNDMENT(9,1)\|EXTERIOR CAPSULE IMPOUNDMENT(9,1)\|GARBAGE IMPOUNDMENT(9,1)\|GRAVITY ASSISTED DRAINAGE PIPE(9,1)\|GRAVITY DRAINAGE ASSISTANCE(9,1)\|INDISCRIMINATE DUMPING(9,1)\|INFRASTRUCTURE SHUTDOWN(9,1)\|MANIPULATED GRADE SHALE(9,1)\|MEDIAN SIZE(9,1)\|SEWAGE IMPOUNDMENT(9,1)\|SUBDIVIDED IMPOUNDMENT(9,1)\|UNTAPPED RESOURCE(9,1)\|WATERPROOF QUALITY ENGINEERING(9,1)\|HEAT PIPE(8,6)\|GUIDELINE(8,3)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CONSTRUCTED SULFUR CAPSULE(8,2)\|IMPOUNDMENT HEIGHT(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MILLING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|VOID VOLUME(7,4)\|CORE DRILLING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|LEAN SHALE(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|LIQUID PRODUCT(6,10)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|CONVECTIVE HEATING(6,2)\|CRUSHED GLASS(6,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(6,2)\|HEATED CONDUIT(6,2)\|HEATING(6,2)\|HORIZONTAL MINING(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|CARBONATE DECOMPOSITION(6,1)\|CO2 EMISSION(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|HYDROGEN DONOR(5,6)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|ANTHEM DEGREE(5,2)\|BLASTING(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|FLOOR CONSTRUCTION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|KEROGEN OIL(4,4)\|HEATED FLUID(4,3)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|PIPING(4,3)\|ANAEROBIC CONDITION(4,1)\|AQUEOUS SLURRY(4,1)\|BARRIER MANUFACTURE(4,1)\|CAPACITY INDICATOR(4,1)\|CAPSULE IMPOUNDMENT AREA(4,1)\|CATALYZING GAS(4,1)\|CEILING CAP(4,1)\|CLAY PIPE(4,1)\|COMMINUTED MASS(4,1)\|COMPOSITION ADMIXTURE(4,1)\|CONCRETE PANEL(4,1)\|CONDUCTIVE CEMENT(4,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(4,1)\|CONSTRUCTED IMPOUNDMENT(4,1)\|DECREASED VISCOSITY(4,1)\|DISPERSION FLUID SENSOR(4,1)\|DUST PARTICLE(4,1)\|ECONOMICALLY VIABLE SOURCE(4,1)\|FAST RECOVERY(4,1)\|FINE COLLECTION(4,1)\|FLUID DRAINAGE(4,1)\|FLUSHING GAS(4,1)\|GAS COMBUSTION HEATER(4,1)\|GASEOUS HYDROCARBON PRODUCT(4,1)\|GEO MEMBRANE LAYER(4,1)\|GEO SYNTHETIC MEMBRANE(4,1)\|GEOLOGICAL LOCATION(4,1)\|HEATING CONDUIT PLACEMENT(4,1)\|HOTSPOT LOCALIZATION(4,1)\|HYDROCARBON VAPOR(4,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(4,1)\|HYDRODESULFURIZATION(4,1)\|IMPOUNDMENT USEFUL LIFE(4,1)\|INORGANIC MATTER(4,1)\|KEROGEN REMOVAL(4,1)\|LAYER COMPACTION(4,1)\|MICROBIOLOGY(4,1)\|MINIMAL WASTE(4,1)\|MINING HAUL TRUCK NEED(4,1)\|MOLTEN CARBONATE FUEL CELL(4,1)\|MONITORING HEAT(4,1)\|NONHEATED BUFFER ZONE(4,1)\|NONOXIDIZING GAS(4,1)\|OIL BLEND(4,1)\|OPTIMIZATION REASON(4,1)\|PIPELINE EXTENSION(4,1)\|PLANT FIBER CELLULOSE(4,1)\|POLYMERIC RESIN(4,1)\|PRECAST PIECE(4,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(4,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(4,1)\|QUALITY DETERIORATION(4,1)\|RECOVERED HYDROCARBON LIQUID(4,1)\|RECOVERING OIL(4,1)\|REFORMATION(4,1)\|RESIDUAL HYDROCARBON PRODUCT(4,1)\|RESIDUAL SHALE REDUCED WETTING(4,1)\|RICH OIL BEARING ORE(4,1)\|ROTATING RETORT(4,1)\|SAND PARTICLE(4,1)\|SEQUENTIAL SOLUTION RECOVERY(4,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(4,1)\|SOLVENT SUBSTITUTED COMPOUND(4,1)\|STAGED PROCESSING(4,1)\|STEAM INJECTION(4,1)\|TECHNICAL CHALLENGE(4,1)\|TREMENDOUS VOLUME(4,1)\|UNCONTROLLED ESCAPE PREVENTION(4,1)\|UNCONTROLLED MIGRATION PREVENTION(4,1)\|VAPOROUS COMPONENT(4,1)\|VARIED ENZYME(4,1)\|VOLATILE ORGANIC(4,1)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOLEACHING(3,1)\|BIOMATERIAL(3,1)\|BIOOXIDATION(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ECONOMICS(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|EXCLUSION(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCLUSION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|LAYER CONDUIT(3,1)\|LAYING WIRE(3,1)\|LIGHTER(3,1)\|LIMITED COMBUSTION INTENT(3,1)\|LIQUID CONDENSATION(3,1)\|LIQUID EMULSION(3,1)\|LUBRICANT COOLANT(3,1)\|\|(IN1891/MUMNP/2011)\|HYDROCARBONACEOUS MATERIAL(100,44)\|INFRASTRUCTURE(100,22)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,13)\|CONSTRUCTED PERMEABILITY(100,12)\|RECOVERING HYDROCARBON(100,12)\|ENCAPSULATED VOLUME(88,24)\|GASEOUS FLUID(60,5)\|GASEOUS COMPONENT(54,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(51,6)\|FLUSH RESIDUAL HYDROCARBON(39,1)\|FLUSH HYDROCARBON VAPOR(38,1)\|COLLECTING REMOVED HYDROCARBON(37,1)\|CONTROL INFRASTRUCTURE(31,21)\|HYDROCARBON COMBUSTION(28,2)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|PERMEABILITY CONTROL IMPOUNDMENT(26,4)\|HYDROCARBONACEOUS MATERIAL FLUSHING(26,1)\|GASEOUS MATERIAL(22,3)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|VOID SPACE(20,5)\|MALFUNCTION(20,1)\|SECTIONED CAPSULE IMPOUNDMENT(19,2)\|STOICHIOMETRIC CONDITION(19,2)\|TOTAL VOLUME(18,2)\|COMPACTED FILL CEILING(17,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(17,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|HEATED HYDROCARBONACEOUS MATERIAL(15,1)\|QUARRY CAPSULE IMPOUNDMENT(15,1)\|UNCAPPED CAPSULE IMPOUNDMENT(15,1)\|UNDERGROUND RUBBLE CHIMNEY(15,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(14,1)\|NANOCARBON FULLERENE ADDITIVE(14,1)\|STRUCTURED IMPOUNDMENT CAPSULE(14,1)\|HYDROCARBON PRODUCTION(13,11)\|PROPANE(12,6)\|CONTAINMENT CAPSULE(12,2)\|NEARBY IMPOUNDMENT(12,2)\|TAILING BERM(12,2)\|UNRECOVERED HYDROCARBON(12,2)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|COAL(11,7)\|PEAT(11,4)\|ENGINEERED PERMEABILITY BARRIER(11,1)\|HYDROCARBON UNCONTROLLED EGRESS(11,1)\|UNDERGROUND MINED HYDROCARBON(11,1)\|BENTONITE CLAY(10,2)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|BENCH MINING ELEVATION(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|EXTERIOR CAPSULE IMPOUNDMENT(10,1)\|GARBAGE IMPOUNDMENT(10,1)\|GRAVITY ASSISTED DRAINAGE PIPE(10,1)\|GRAVITY DRAINAGE ASSISTANCE(10,1)\|INDISCRIMINATE DUMPING(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|MANIPULATED GRADE SHALE(10,1)\|MEDIAN SIZE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|UNTAPPED RESOURCE(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|HEAT PIPE(9,6)\|CONSTRUCTED SULFUR CAPSULE(9,2)\|IMPOUNDMENT HEIGHT(9,2)\|VOID VOLUME(8,4)\|GUIDELINE(8,3)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CORE DRILLING(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MINING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|LIQUID PRODUCT(7,10)\|CONVECTIVE HEATING(7,2)\|CRUSHED GLASS(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HEATED CONDUIT(7,2)\|HEATING(7,2)\|HORIZONTAL MINING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|BIO LEACHING(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|LEAN SHALE(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|HYDROGEN DONOR(6,6)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|FLOOR CONSTRUCTION(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|CARBONATE DECOMPOSITION(6,1)\|CO2 EMISSION(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|KEROGEN OIL(5,4)\|HEATED FLUID(5,3)\|PIPING(5,3)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|BLASTING(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|ANAEROBIC CONDITION(5,1)\|AQUEOUS SLURRY(5,1)\|BARRIER MANUFACTURE(5,1)\|CAPACITY INDICATOR(5,1)\|CAPSULE IMPOUNDMENT AREA(5,1)\|CATALYZING GAS(5,1)\|CEILING CAP(5,1)\|CLAY PIPE(5,1)\|CO2 PRODUCTION(5,1)\|COMMINUTED MASS(5,1)\|COMPOSITION ADMIXTURE(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|DECREASED VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLUID DRAINAGE(5,1)\|FLUSHING GAS(5,1)\|GAS COMBUSTION HEATER(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GEO MEMBRANE LAYER(5,1)\|GEO SYNTHETIC MEMBRANE(5,1)\|GEOLOGICAL LOCATION(5,1)\|HEATING CONDUIT PLACEMENT(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBON VAPOR(5,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|IMPOUNDMENT USEFUL LIFE(5,1)\|INORGANIC MATTER(5,1)\|KEROGEN REMOVAL(5,1)\|LAYER COMPACTION(5,1)\|MICROBIOLOGY(5,1)\|MINIMAL WASTE(5,1)\|MINING HAUL TRUCK NEED(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONOXIDIZING GAS(5,1)\|OIL BLEND(5,1)\|OPTIMIZATION REASON(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PRECAST PIECE(5,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(5,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(5,1)\|QUALITY DETERIORATION(5,1)\|RECOVERED HYDROCARBON LIQUID(5,1)\|RECOVERING OIL(5,1)\|REFORMATION(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RESIDUAL SHALE REDUCED WETTING(5,1)\|RICH OIL BEARING ORE(5,1)\|ROTATING RETORT(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|STAGED PROCESSING(5,1)\|STEAM INJECTION(5,1)\|TECHNICAL CHALLENGE(5,1)\|TREMENDOUS VOLUME(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNCONTROLLED MIGRATION PREVENTION(5,1)\|VAPOROUS COMPONENT(5,1)\|VARIED ENZYME(5,1)\|VOLATILE ORGANIC(5,1)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOMATERIAL(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ECONOMICS(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|LAYER CONDUIT(3,1)\|LAYING WIRE(3,1)\|LIGHTER(3,1)\|LIMITED COMBUSTION INTENT(3,1)\|LIQUID CONDENSATION(3,1)\|LIQUID EMULSION(3,1)\|LUBRICANT COOLANT(3,1)\|\|(CA2752133)\|HYDROCARBONACEOUS MATERIAL(100,45)\|INFRASTRUCTURE(100,22)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,13)\|CONSTRUCTED PERMEABILITY(100,12)\|RECOVERING HYDROCARBON(100,12)\|ENCAPSULATED VOLUME(87,25)\|GASEOUS FLUID(60,5)\|GASEOUS COMPONENT(54,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(51,6)\|FLUSH RESIDUAL HYDROCARBON(39,1)\|FLUSH HYDROCARBON VAPOR(38,1)\|COLLECTING REMOVED HYDROCARBON(37,1)\|CONTROL INFRASTRUCTURE(31,21)\|HYDROCARBON COMBUSTION(28,2)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|PERMEABILITY CONTROL IMPOUNDMENT(26,4)\|HYDROCARBONACEOUS MATERIAL FLUSHING(26,1)\|GASEOUS MATERIAL(22,3)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|VOID SPACE(20,5)\|MALFUNCTION(20,1)\|SECTIONED CAPSULE IMPOUNDMENT(19,2)\|STOICHIOMETRIC CONDITION(19,2)\|TOTAL VOLUME(18,2)\|COMPACTED FILL CEILING(17,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(17,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|HEATED HYDROCARBONACEOUS MATERIAL(15,1)\|QUARRY CAPSULE IMPOUNDMENT(15,1)\|UNCAPPED CAPSULE IMPOUNDMENT(15,1)\|UNDERGROUND RUBBLE CHIMNEY(15,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(14,1)\|NANOCARBON FULLERENE ADDITIVE(14,1)\|STRUCTURED IMPOUNDMENT CAPSULE(14,1)\|HYDROCARBON PRODUCTION(13,11)\|PROPANE(12,6)\|CONTAINMENT CAPSULE(12,2)\|NEARBY IMPOUNDMENT(12,2)\|TAILING BERM(12,2)\|UNRECOVERED HYDROCARBON(12,2)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|COAL(11,7)\|PEAT(11,4)\|ENGINEERED PERMEABILITY BARRIER(11,1)\|HYDROCARBON UNCONTROLLED EGRESS(11,1)\|UNDERGROUND MINED HYDROCARBON(11,1)\|BENTONITE CLAY(10,2)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|BENCH MINING ELEVATION(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|EXTERIOR CAPSULE IMPOUNDMENT(10,1)\|GARBAGE IMPOUNDMENT(10,1)\|GRAVITY ASSISTED DRAINAGE PIPE(10,1)\|GRAVITY DRAINAGE ASSISTANCE(10,1)\|INDISCRIMINATE DUMPING(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|MANIPULATED GRADE SHALE(10,1)\|MEDIAN SIZE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|UNTAPPED RESOURCE(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|HEAT PIPE(9,6)\|CONSTRUCTED SULFUR CAPSULE(9,2)\|IMPOUNDMENT HEIGHT(9,2)\|VOID VOLUME(8,4)\|GUIDELINE(8,3)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CORE DRILLING(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MINING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|LIQUID PRODUCT(7,10)\|CONVECTIVE HEATING(7,2)\|CRUSHED GLASS(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HEATED CONDUIT(7,2)\|HEATING(7,2)\|HORIZONTAL MINING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|LEAN SHALE(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|HYDROGEN DONOR(6,6)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|FLOOR CONSTRUCTION(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|ACID HALIDE(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|CARBONATE DECOMPOSITION(6,1)\|CO2 EMISSION(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|RESIN ION EXCHANGE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|KEROGEN OIL(5,4)\|HEATED FLUID(5,3)\|PIPING(5,3)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|BLASTING(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|ANAEROBIC CONDITION(5,1)\|AQUEOUS SLURRY(5,1)\|BARRIER MANUFACTURE(5,1)\|CAPACITY INDICATOR(5,1)\|CAPSULE IMPOUNDMENT AREA(5,1)\|CATALYZING GAS(5,1)\|CEILING CAP(5,1)\|CLAY PIPE(5,1)\|CO2 PRODUCTION(5,1)\|COMMINUTED MASS(5,1)\|COMPOSITION ADMIXTURE(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|DECREASED VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLUID DRAINAGE(5,1)\|FLUSHING GAS(5,1)\|GAS COMBUSTION HEATER(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GEO MEMBRANE LAYER(5,1)\|GEO SYNTHETIC MEMBRANE(5,1)\|GEOLOGICAL LOCATION(5,1)\|HEATING CONDUIT PLACEMENT(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBON VAPOR(5,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|IMPOUNDMENT USEFUL LIFE(5,1)\|INORGANIC MATTER(5,1)\|KEROGEN REMOVAL(5,1)\|LAYER COMPACTION(5,1)\|MICROBIOLOGY(5,1)\|MINIMAL WASTE(5,1)\|MINING HAUL TRUCK NEED(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONOXIDIZING GAS(5,1)\|OIL BLEND(5,1)\|OPTIMIZATION REASON(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PRECAST PIECE(5,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(5,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(5,1)\|QUALITY DETERIORATION(5,1)\|RECOVERED HYDROCARBON LIQUID(5,1)\|RECOVERING OIL(5,1)\|REFORMATION(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RESIDUAL SHALE REDUCED WETTING(5,1)\|RICH OIL BEARING ORE(5,1)\|ROTATING RETORT(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|STAGED PROCESSING(5,1)\|STEAM INJECTION(5,1)\|TECHNICAL CHALLENGE(5,1)\|TREMENDOUS VOLUME(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNCONTROLLED MIGRATION PREVENTION(5,1)\|VAPOROUS COMPONENT(5,1)\|VARIED ENZYME(5,1)\|VOLATILE ORGANIC(5,1)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOLEACHING(3,1)\|BIOMATERIAL(3,1)\|BIOOXIDATION(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ECONOMICS(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|ELECTROPLATING(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLOTATION(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|LAYER CONDUIT(3,1)\|LAYING WIRE(3,1)\|LIGHTER(3,1)\|LIMITED COMBUSTION INTENT(3,1)\|LIQUID CONDENSATION(3,1)\|LIQUID EMULSION(3,1)\|	(US8349171)\|What is claimed is:\|1. A method of recovering hydrocarbons from hydrocarbonaceous materials, comprising:\| a) forming a constructed permeability control infrastructure which defines a substantially encapsulated volume;\| b) introducing a comminuted hydrocarbonaceous material into the control infrastructure to form a permeable body of hydrocarbonaceous material;\| c) maintaining within said encapsulated volume a positive pressure relative to the pressure outside of said control infrastructure;\| d) heating the hydrocarbonaceous material sufficient to remove hydrocarbons therefrom such that the hydrocarbonaceous material is substantially stationary during heating;\| e) flushing a gaseous fluid substantially free of oxygen throughout the permeable body in order to substantially remove hydrocarbons and other gaseous components from the permeable body, wherein heating of said hydrocarbonaceous materials has been terminated and said gaseous fluid is passed throughout the permeable body at a low temperature relative to the temperature at which said hydrocarbonaceous materials have been heated to provide a cooling effect on said hydrocarbonaceous materials and flush residual hydrocarbons and other gaseous materials from within said encapsulated volume; and\| f) collecting removed hydrocarbons and other gaseous components.\|2. The method of claim 1, wherein the hydrocarbonaceous material comprises oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof.\|3. The method of claim 1, wherein the hydrocarbonaceous material comprises oil shale.\|4. The method of claim 1, wherein the permeable body consists essentially of crushed hydrocarbonaceous material having an average size from about 6 inches to about 2 feet.\|5. The method of claim 1, wherein the permeable body has a void space from about 10% to about 50% a total volume of the permeable body.\|6. The method of claim 1, wherein the permeable body has a void space from about 30% to about 45% a total volume of the permeable body.\|7. The method of claim 1, wherein the positive pressure is maintained by means of a plurality of conduits at least some of which are embedded within the permeable body and wherein at least some of said conduits are configured to introduce said gaseous fluid at a predetermined temperature so as to cause heating or cooling of said hydrocarbonaceous material.\|8. The method of claim 1, wherein said heating has been terminated as a result of the release of unwanted hydrocarbons of other gaseous materials due to a malfunction.\|9. The method of claim 1, wherein said heating has been terminated as a result of the removal of effectively recoverable amounts of hydrocarbons from said hydrocarbonaceous materials and said flushing continues for a time sufficient to allow removal of remaining volumes of recoverable hydrocarbons and other gaseous materials and the cooling of said hydrocarbonaceous materials.\|10. The method of claim 1, wherein said gaseous fluid is a member selected from the group consisting of hydrogen, nitrogen, propane, carbon dioxide, hydrocarbons, and combinations thereof.\|11. The method of claim 1, wherein the positive pressure is from about 1.01 atm to about 10 atm.\|12. The method of claim 1, wherein the positive pressure is from about 1.1 atm to about 4 atm.\|13. The method of claim 1, wherein heating of the permeable body is accomplished by hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen.\|14. The method of claim 1, wherein the constructed permeability control infrastructure comprises clay, bentonite clay, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon, filled geotextile bags, polymeric resins, or combinations thereof.\|15. The method of claim 1, wherein the constructed permeability control infrastructure has a foundation structural floor support of earthen material or local surface topography as a floor.\|16. A constructed permeability control infrastructure, comprising:\| a) a permeability control impoundment defining a substantially encapsulated volume, said impoundment having a foundation structural floor support of earthen material or local surface topography as a floor; and\| b) a comminuted hydrocarbonaceous material within the encapsulated volume forming a substantially stationary permeable body of hydrocarbonaceous material, wherein the impoundment is adapted such that a positive pressure is maintained in said encapsulated volume relative to the pressure outside of said control infrastructure and prevents the introduction of air or other oxidizing gases from entering the impoundment.\|17. The constructed permeability control infrastructure of claim 16, wherein the constructed permeability control infrastructure comprises clay, bentonite clay, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon, filled geotextile bags, polymeric resins, or combinations thereof.	(US8349171)\|RELATED APPLICATION\|[0001] This application claims priority to U.S. Provisional Patent Application No. 61/152,146, filed Feb. 12, 2009, which is incorporated herein by reference.\|(US8349171)\|BACKGROUND\|[0002] Global and domestic demand for fossil fuels continues to rise despite price increases and other economic and geopolitical concerns. As such demand continues to rise, research and investigation into finding additional economically viable sources of fossil fuels correspondingly increases. Historically, many have recognized the vast quantities of energy stored in oil shale, coal and tar sand deposits, for example. However, these sources remain a difficult challenge in terms of economically competitive recovery. Canadian tar sands have shown that such efforts can be fruitful, although many challenges still remain, including environmental impact, product quality, production costs and process time, among others.\|[0003] Estimates of world-wide oil shale reserves range from two to almost seven trillion barrels of oil, depending on the estimating source. Regardless, these reserves represent a tremendous volume and remain a substantially untapped resource. A large number of companies and investigators continue to study and test methods of recovering oil from such reserves. In the oil shale industry, methods of extraction have included underground rubble chimneys created by explosions, in-situ methods such as In-Situ Conversion Process (ICP) method (Shell Oil), and heating within steel fabricated retorts. Other methods have included in-situ radio frequency methods (microwaves), and “modified” in-situ processes wherein underground mining, blasting and retorting have been combined to make rubble out of a formation to allow for better heat transfer and product removal.\|[0004] Among typical oil shale processes, all face tradeoffs in economics and environmental concerns. No current process alone satisfies economic, environmental and technical challenges. Moreover, global warming concerns give rise to additional measures to address carbon dioxide (CO2) emissions which are associated with such processes. Methods are needed that accomplish environmental stewardship, yet still provide high-volume cost-effective oil production.\|[0005] Below ground in-situ concepts emerged based on their ability to produce high volumes while avoiding the cost of mining. While the cost savings resulting from avoiding mining can be achieved, the in-situ method requires heating a formation for a longer period of time due to the extremely low thermal conductivity and high specific heat of solid oil shale. Perhaps the most significant challenge for any in-situ process is the uncertainty and long term potential of water contamination that can occur with underground freshwater aquifers. In the case of Shell's ICP method, a “freeze wall” is used as a barrier to keep separation between aquifers and an underground treatment area. Although this is possible, no long term analysis has proven for extended periods to guarantee the prevention of contamination. Without guarantees and with even fewer remedies should a freeze wall fail, other methods are desirable to address such environmental risks.\|[0006] For this and other reasons, the need remains for methods and systems which can provide improved recovery of hydrocarbons from suitable hydrocarbon-containing materials, which have acceptable economics and avoid the drawbacks mentioned above.\|SUMMARY\|[0007] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating the hydrocarbonaceous material can be substantially stationary. Removed fluid hydrocarbons can be collected for further processing, use in the process as supplemental fuel or additives, and/or direct use without further treatment.\|[0008] These systems and processes can allow difficult problems to be solved related to the extraction of hydrocarbon liquids and gases from surface or underground mined hydrocarbon bearing deposits such as oil shale, tar sands, lignite, and coal, and from harvested biomass. Among other things, this approach helps reduce cost, increase volume output, lower air emissions, limit water consumption, prevent underground aquifer contamination, reclaim surface disturbances, reduce material handling costs, remove dirty fine particulates, and improve composition of recovered hydrocarbon liquid or gas. It also addresses water contamination issues with a safer, more predictable, engineered, observable, repairable, adaptable and preventable water protection structure.\|[0009] Additional features and advantages of the invention will be apparent from the following detailed description, which illustrates, by way of example, features of the invention.\|(US8349171)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0010] FIG. 1 is side partial cutaway view schematic of a constructed permeability control infrastructure in accordance with one embodiment.\|[0011] FIGS. 2A and 2B are top and plan views of a plurality of permeability control impoundments in accordance with one embodiment.\|[0012] FIG. 3 is a side cutaway view of a permeability control impoundment in accordance with one embodiment.\|[0013] FIG. 4 is a schematic of a portion of a constructed infrastructure in accordance with an embodiment.\|[0014] FIG. 5 is a schematic showing heat transfer between two permeability control impoundments in accordance with another embodiment.\|(US8349171)\|DETAILED DESCRIPTION\|[0015] It should be noted that the figures are merely exemplary of several embodiments and no limitations on the scope of the present invention are intended thereby. Further, the figures are generally not drawn to scale, but are drafted for purposes of convenience and clarity in illustrating various aspects of the invention.\|DETAILED DESCRIPTION\|[0016] Reference will now be made to exemplary embodiments and specific language will be used herein to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended. Alterations and further modifications of the inventive features described herein, and additional applications of the principles of the invention as described herein, which would occur to one skilled in the relevant art and having possession of this disclosure, are to be considered within the scope of the invention. Further, before particular embodiments are disclosed and described, it is to be understood that this invention is not limited to the particular process and materials disclosed herein as such may vary to some degree. It is also to be understood that the terminology used herein is used for the purpose of describing particular embodiments only and is not intended to be limiting, as the scope of the present invention will be defined only by the appended claims and equivalents thereof.\|DEFINITIONS\|[0017] In describing and claiming the present invention, the following terminology will be used.\|[0018] The singular forms “a,” “an,” and “the” include plural references unless the context clearly dictates otherwise. Thus, for example, reference to “a wall” includes reference to one or more of such structures, “a permeable body” includes reference to one or more of such materials, and “a heating step” refers to one or more of such steps.\|[0019] As used herein “existing grade” or similar terminology refers to the grade or a plane parallel to the local surface topography of a site containing an infrastructure as described herein which infrastructure may be above or below the existing grade.\|[0020] As used herein, “conduits” refers to any passageway along a specified distance which can be used to transport materials and/or heat from one point to another point. Although conduits can generally be circular pipes, other non-circular conduits can also be useful. Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|[0021] As used herein, “constructed infrastructure” refers to a structure which is substantially entirely man made, as opposed to freeze walls, sulfur walls, or other barriers which are formed by modification or filling pores of an existing geological formation.\|[0022] The constructed permeability control infrastructure is often substantially free of undisturbed geological formations, although the infrastructure can be formed adjacent or in direct contact with an undisturbed formation. Such a control infrastructure can be unattached or affixed to an undisturbed formation by mechanical means, chemical means or a combination of such means, e.g. bolted into the formation using anchors, ties, or other suitable hardware.\|[0023] As used herein, “comminuted” refers to breaking a formation or larger mass into pieces. A comminuted mass can be rubbilized or otherwise broken into fragments.\|[0024] As used herein, “hydrocarbonaceous material” refers to any hydrocarbon-containing material from which hydrocarbon products can be extracted or derived. For example, hydrocarbons may be extracted directly as a liquid, removed via solvent extraction, directly vaporized or otherwise removed from the material. However, many hydrocarbonaceous materials contain kerogen or bitumen which is converted to a hydrocarbon through heating and pyrolysis. Hydrocarbonaceous materials can include, but is not limited to, oil shale, tar sands, coal, lignite, bitumen, peat, and other organic materials.\|[0025] As used herein, “impoundment” refers to a structure designed to hold or retain an accumulation of fluid and/or solid moveable materials. An impoundment generally derives at least a substantial portion of foundation and structural support from earthen materials. Thus, the control walls do not always have independent strength or structural integrity apart from the earthen material and/or formation against which they are formed.\|[0026] As used herein, “permeable body” refers to any mass of comminuted hydrocarbonaceous material having a relatively high permeability which exceeds permeability of a solid undisturbed formation of the same composition. Suitable permeable bodies can have greater than about 10% void space and typically have void space from about 30% to 45%, although other ranges may be suitable. Allowing for high permeability facilitates, for example, through the incorporation of large irregularly shaped particles, heating of the body through convection as the primary heat transfer while also substantially reducing costs associated with crushing to very small sizes, e.g. below about 1 to about 0.5 inch.\|[0027] As used herein, “wall” refers to any constructed feature having a permeability control contribution to confining material within an encapsulated volume defined at least in part by control walls. Walls can be oriented in any manner such as vertical, although ceilings, floors and other contours defining the encapsulated volume can also be “walls” as used herein.\|[0028] As used herein, “mined” refers to a material which has been removed or disturbed from an original stratographic or geological location to a second and different location or returned to the same location. Typically, mined material can be produced by rubbilizing, crushing, explosively detonating, or otherwise removing material from a geologic formation.\|[0029] As used herein, “substantially stationary” refers to nearly stationary positioning of materials with a degree of allowance for subsidence, expansion, and/or settling as hydrocarbons are removed from the hydrocarbonaceous material from within the enclosed volume to leave behind lean material. In contrast, any circulation and/or flow of hydrocarbonaceous material such as that found in fluidized beds or rotating retorts involves highly substantial movement and handling of hydro carbonaceous material.\|[0030] As used herein, “substantial” when used in reference to a quantity or amount of a material, or a specific characteristic thereof, refers to an amount that is sufficient to provide an effect that the material or characteristic was intended to provide. The exact degree of deviation allowable may in some cases depend on the specific context. Similarly, “substantially free of” or the like refers to the lack of an identified element or agent in a composition. Particularly, elements that are identified as being “substantially free of” are either completely absent from the composition, or are included only in amounts which are small enough so as to have no measurable effect on the composition.\|[0031] As used herein, “about” refers to a degree of deviation based on experimental error typical for the particular property identified. The latitude provided the term “about” will depend on the specific context and particular property and can be readily discerned by those skilled in the art. The term “about” is not intended to either expand or limit the degree of equivalents which may otherwise be afforded a particular value. Further, unless otherwise stated, the term “about” shall expressly include “exactly,” consistent with the discussion below regarding ranges and numerical data.\|[0032] Concentrations, dimensions, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of about 1 to about 200 should be interpreted to include not only the explicitly recited limits of 1 and 200, but also to include individual sizes such as 2, 3, 4, and sub-ranges such as 10 to 50, 20 to 100, etc.\|[0033] As used herein, a plurality of items, structural elements, compositional elements, and/or materials may be presented in a common list for convenience. However, these lists should be construed as though each member of the list is individually identified as a separate and unique member. Thus, no individual member of such list should be construed as a de facto equivalent of any other member of the same list solely based on their presentation in a common group without indications to the contrary.\|[0034] Recovering Hydrocarbons from Hydrocarbonaceous Materials Under Positive Pressure\|[0035] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined or harvested hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure is a fixed structure. Removed fluid hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.\|[0036] The constructed permeability control infrastructure can be formed using existing grade as floor support and/or as side wall support for the constructed infrastructure. For example, the control infrastructure can be formed as a free standing structure, i.e. using only existing grade as a floor with side walls being man-made. Alternatively, the control infrastructure can be formed within an excavated pit.\|[0037] A constructed permeability control infrastructure can include a permeability control impoundment which defines a substantially encapsulated volume. The permeability control impoundment is substantially free of undisturbed geological formations. Specifically, the permeability control aspect of the impoundment can be completely constructed and manmade as a separate isolation mechanism for prevention of uncontrolled migration of material into or out of the encapsulated volume.\|[0038] In one embodiment, the permeability control impoundment can be formed along walls of an excavated hydrocarbonaceous material deposit. For example, oil shale, tar sands, or coal can be mined from a deposit to form a cavity which corresponds approximately to a desired encapsulation volume for an impoundment. The excavated cavity can then be used as a form and support to create the permeability control impoundment.\|[0039] In one alternative aspect, at least one additional excavated hydrocarbonaceous material deposit can be formed such that a plurality of impoundments can be operated. Further, such a configuration can facilitate a reduction in transportation distance of the mined material. Specifically, the mined hydrocarbonaceous material for any particular encapsulated volume can be mined from an adjacent excavated hydrocarbonaceous material deposit. In this manner, a grid of constructed structures can be built such that mined material can be immediately and directly filled into an adjacent impoundment.\|[0040] Mining and/or excavation of hydro carbonaceous deposits can be accomplished using any suitable technique. Conventional surface mining can be used, although alternative excavators can also be used without requirement of transportation of the mined materials. In one specific embodiment, the hydrocarbonaceous deposit can be excavated using a crane-suspended excavator. One example of a suitable excavator can include vertical tunnel boring machines. Such machines can be configured to excavate rock and material beneath the excavator. As material is removed, the excavator is lowered to ensure substantially continuous contact with a formation. Removed material can be conveyed out of the excavation area using conveyors or lifts. Alternatively, the excavation can occur under aqueous slurry conditions to reduce dust problems and act as a lubricant/coolant. The slurry material can be pumped out of the excavation for separation of solids in a settling tank or other similar solid-liquid separator, or the solids may be allowed to precipitate directly in an impoundment. This approach can be readily integrated with simultaneous or sequential solution-based recovery of metals and other materials as described in more detail below.\|[0041] Further, excavation and formation of a permeability control impoundment can be accomplished simultaneously. For example, an excavator can be configured to remove hydro carbonaceous material while side walls of an impoundment are formed. Material can be removed from just underneath edges of the side walls such that the walls can be guided downward to allow additional wall segments to be stacked above. This approach can allow for increased depths while avoiding or reducing dangers of cave-in prior to formation of supporting impoundment walls.\|[0042] The impoundment can be formed of any suitable material which provides isolation of material transfer across walls of the impoundment. In this manner, integrity of the walls is retained during operation of the control infrastructure sufficient to substantially prevent uncontrolled migration of fluids outside of the control infrastructure. Non-limiting examples of suitable material for use in forming the impoundment of the constructed permeability control infrastructure can include clay, bentonite clay (e.g. clay comprising at least a portion of bentonite), bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, or combinations thereof. Engineered cementitious composites (ECC) materials, fiber reinforced composites, and the like can be particularly strong and can be readily engineered to meet permeability and temperature tolerance requirements of a given installation. As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required. For example, materials having a melting point above the maximum operating temperature of the infrastructure can be useful to maintain containment during and after heating and recovery. However, lower temperature materials can also be used if a non-heated buffer zone is maintained between the walls and heated portions of the permeable body. Such buffer zones can range from 6 inches to 50 feet depending on the particular material used for the impoundment and the composition of the permeable body. In another aspect, walls of the impoundment can be acid, water and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water. For impoundment walls formed along formations or other solid support, the impoundment walls can be formed of a sprayed grouting, sprayed liquid emulsions, or other sprayed material such as sprayable refractory grade grouting which forms a seal against the formation and creates the permeability control wall of the impoundments. Impoundment walls may be substantially continuous such that the impoundment defines the encapsulated volume sufficiently to prevent substantial movement of fluids into or out of the impoundment other than defined inlets and outlets, e.g. via conduits or the like as discussed herein. In this manner, the impoundments can readily meet government fluid migration regulations. Alternatively, or in combination with a manufactured barrier, portions of the impoundment walls can be undisturbed geological formation and/or compacted earth. In such cases, the constructed permeability control infrastructure is a combination of permeable and impermeable walls as described in more detail below.\|[0043] In one detailed aspect, a portion of hydrocarbonaceous material, either pre- or post-processed, can be used as a cement fortification and/or cement base which are then poured in place to form portions or the entirety of walls of the control infrastructure. These materials can be formed in place or can be preformed and then assembled on site to form an integral impoundment structure. For example, the impoundment can be constructed by cast forming in place as a monolithic body, extrusion, stacking of preformed or precast pieces, concrete panels joined by a grout (cement, ECC or other suitable material), inflated form, or the like. The forms can be built up against a formation or can be stand alone structures. Forms can be constructed of any suitable material such as, but not limited to, steel, wood, fiberglass, polymer, or the like. The forms can be assembled in place or may be oriented using a crane or other suitable mechanism. Alternatively, the constructed permeability control infrastructure can be formed of gabions and/or geosynthetic fabrics assembled in layers with compacted fill material. Optional binders can be added to enhance compaction of the permeability control walls. In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|[0044] Impoundment walls can optionally include non-permeable insulation and/or fines collection layers. These permeable layers can be oriented between the permeability control barrier and the permeable body. For example, a layer of hydrocarbonaceous comminuted material can be provided which allows fluids to enter, cool, and at least partially condense within the layer. Such permeable layer material can generally have a particle size smaller than the permeable body. Further, such hydrocarbonaceous material can remove fines from passing fluids via various attractive forces. In one embodiment, the construction of impoundment walls and floors can include multiple compacted layers of indigenous or manipulated low grade shale with any combination of sand, cement, fiber, plant fiber, nano carbons, crushed glass, reinforcement steel, engineered carbon reinforcement grid, calcium salts, and the like. In addition to such composite walls, designs which inhibit long term fluid and gas migration through additional impermeability engineering can be employed including, but not limited to, liners, geo-membranes, compacted soils, imported sand, gravel or rock and gravity drainage contours to move fluids and gases away from impervious layers to egress exits. Impoundment floor and wall construction, can, but need not comprise, a stepped up or stepped down slope or bench as the case of mining course may dictate following the optimal ore grade mining. In any such stepped up or down applications, floor leveling and containment wall construction can typically drain or slope to one side or to a specific central gathering area(s) for removal of fluids by gravity drainage assistance.\|[0045] Optionally, capsule wall and floor construction can include insulation which prevents heat transfer outside of the constructed infrastructure or outside of inner capsules or conduits within the primary constructed capsule containment. Insulation can comprise manufactured materials, cement or various materials other materials which are less thermally conductive than surrounding masses, i.e. permeable body, formation, adjacent infrastructures, etc. Thermally insulating barriers can also be formed within the permeable body, along impoundment walls, ceilings and/or floors. One detailed aspect includes the use of biodegradable insulating materials, e.g. soy insulation and the like. This is consistent with embodiments wherein the impoundment is a single use system such that insulations, pipes, and/or other components can have a relatively low useful life, e.g. less than 1-2 years. This can reduce equipment costs as well as reduce long-term environmental impact.\|[0046] These structures and methods can be applied at almost any scale. Larger encapsulated volumes and increased numbers of impoundments can readily produce hydrocarbon products and performance comparable to or exceeding smaller constructed infrastructures. As an illustration, single impoundments can range in size from tens of meters across to tens of acres. Optimal impoundment sizes may vary depending on the hydrocarbonaceous material and operating parameters, however it is expected that suitable areas can range from about one-half to five acres in top plan surface area.\|[0047] The methods and infrastructures can be used for recovery of hydrocarbons from a variety of hydrocarbonaceous materials. One particular advantage is a wide degree of latitude in controlling particle size, conditions, and composition of the permeable body introduced into the encapsulated volume. Non-limiting examples of mined hydrocarbonaceous material which can be treated comprise oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof. In some cases it can be desirable to provide a single type of hydrocarbonaceous material so that the permeable body consists essentially of one of the above materials. However, the permeable body can include mixtures of these materials such that grade, oil content, hydrogen content, permeability and the like can be adjusted to achieve a desired result. Further, different hydrocarbon materials can be placed in multiple layers or in a mixed fashion such as combining coal, oil shale, tar sands, biomass, and/or peat.\|[0048] In one embodiment, hydrocarbon containing material can be classified into various inner capsules within a primary constructed infrastructure for optimization reasons. For instance, layers and depths of mined oil shale formations may be richer in certain depth pay zones as they are mined. Once, blasted, mined, shoveled and hauled inside of capsule for placement, richer oil bearing ores can be classified or mixed by richness for optimal yields, faster recovery, or for optimal averaging within each impoundment. Further, providing layers of differing composition can have added benefits. For example, a lower layer of tar sands can be oriented below an upper layer of oil shale. Generally, the upper and lower layers can be in direct contact with one another although this is not required. The upper layer can include heating pipes embedded therein as described in more detail below. The heating pipes can heat the oil shale sufficient to liberate kerogen oil, including short-chain liquid hydrocarbons, which can act as a solvent for bitumen removal from the tar sands. In this manner, the upper layer acts as an in situ solvent source for enhancing bitumen removal from the lower layer. Heating pipes within the lower layer are optional such that the lower layer can be free of heating pipes or may include heating pipes, depending on the amount of heat transferred via downward passing liquids from the upper layer and any other heat sources. The ability to selectively control the characteristics and composition of the permeable body adds a significant amount of freedom in optimizing oil yields and quality.\|[0049] Furthermore, in many embodiments, the liberated gaseous and liquid products act as an in situ produced solvent which supplements kerogen removal and/or additional hydrocarbon removal from the hydro carbonaceous material.\|[0050] In yet another detailed aspect, the permeable body can further comprise an additive or biomass. Additives can include any composition which acts to increase the quality of removed hydrocarbons, e.g. increased API, decreased viscosity, improved flow properties, reduced wetting of residual shale, reduction of sulfur, hydrogenation agents, etc. Non-limiting examples of suitable additives can include bitumen, kerogen, propane, natural gas, natural gas condensate, crude oil, refining bottoms, asphaltenes, common solvents, other diluents, and combinations of these materials. In one specific embodiment, the additive can include a flow improvement agent and/or a hydrogen donor agent. Some materials can act as both or either agents to improve flow or as a hydrogen donor. Non-limiting examples of such additives can include methane, natural gas condensates, common solvent such as acetone, toluene, benzene, etc., and other additives listed above. Additives can act to increase the hydrogen to carbon ratio in any hydrocarbon products, as well as act as a flow enhancement agent. For example, various solvents and other additives can create a physical mixture which has a reduced viscosity and/or reduced affinity for particulate solids, rock and the like. Further, some additives can chemically react with hydrocarbons and/or allow liquid flow of the hydrocarbon products. Any additives used can become part of a final recovered product or can be removed and reused or otherwise disposed of.\|[0051] Similarly, biological hydroxylation of hydrocarbonaceous materials to form synthetic gas or other lighter weight products can be accomplished using known additives and approaches. Enzymes or biocatalysts can also be used in a similar manner. Further, manmade materials can also be used as additives such as, but not limited to, tires, polymeric refuse, or other hydrocarbon-containing materials.\|[0052] Although these methods are broadly applicable, as a general guideline, the permeable body can include particles from about ⅛ inch to about 6 feet in largest dimension, and in some cases less than 1 foot and in other cases less than about 6 inches. However, as a practical matter, sizes from about 2 inches to about 2 feet can provide good results with about 1 foot diameter being useful for oil shale especially. Void space can be an important factor in determining optimal particle diameters. As a general matter, any functional void space can be used; however, about 10% to about 50% and in some cases about 30% to about 45% usually provides a good balance of permeability and effective use of available volumes. Void volumes can be varied somewhat by varying other parameters such as heating conduit placement, additives, and the like. Mechanical separation of mined hydrocarbonaceous materials allows creation of fine mesh, high permeability particles which enhance thermal dispersion rates once placed in capsule within the impoundment. The added permeability allows for more reasonable, low temperatures which also help to avoid higher temperatures which result in greater CO2 production from carbonate decomposition and associated release of trace heavy metals, volatile organics, and other compounds which can create toxic effluent and/or undesirable materials which can be monitored and controlled.\|[0053] In one embodiment, computer assisted mining, mine planning, hauling, blasting, assay, loading, transport, placement, and dust control measures can be utilized to fill and optimize the speed of mined material movement into the constructed capsule containment structure. In one alternative aspect, the impoundments can be formed in excavated volumes of a hydrocarbonaceous formation, although other locations remote from the control infrastructure can also be useful. For example, some hydrocarbonaceous formations have relatively thin hydrocarbon-rich layers, e.g. less than about 300 feet thick. Therefore, vertical mining and drilling tend to not be cost effective. In such cases, horizontal mining can be useful to recover the hydrocarbonaceous materials for formation of the permeable body. Although horizontal mining continues to be a challenging endeavor, a number of technologies have been developed and continue to be developed which can be useful in connection with the impoundments. In such cases, at least a portion of the impoundment can be formed across a horizontal layer, while other portions of the impoundment can be formed along and/or adjacent non-hydrocarbon bearing formation layers. Other mining approaches such as, but not limited to, room and pillar mining can provide an effective source of hydrocarbonaceous material with minimal waste and/or reclamation which can be transported to an impoundment and treated in accordance with these principles.\|[0054] As mentioned herein, these systems and processes allow for a large degree of control regarding properties and characteristics of the permeable body which can be designed and optimized for a given installation. Impoundments, individually and across a plurality of impoundments can be readily tailored and classified based on varying composition of materials, intended products and the like. For example, several impoundments can be dedicated to production of heavy crude oil, while others can be configured for production of lighter products and/or syn gas. Non-limiting example of potential classifications and factors can include catalyst activity, enzymatic reaction for specific products, aromatic compounds, hydrogen content, microorganism strain or purpose, upgrading process, target final product, pressure (effects product quality and type), temperature, swelling behavior, aquathermal reactions, hydrogen donor agents, heat superdisposition, garbage impoundment, sewage impoundment, reusable pipes, and others. Typically, a plurality of these factors can be used to configure impoundments in a given project area for distinct products and purposes.\|[0055] The comminuted hydrocarbonaceous material can be filled into the control infrastructure to form the permeable body in any suitable manner. Typically the comminuted hydrocarbonaceous material can be conveyed into the control infrastructure by dumping, conveyors or other suitable approaches. As mentioned previously, the permeable body can have a suitably high void volume. Indiscriminate dumping can result in excessive compaction and reduction of void volumes. Thus, the permeable body can be formed by low compaction conveying of the hydrocarbonaceous material into the infrastructure. For example, retracting conveyors can be used to deliver the material near a top surface of the permeable body as it is formed. In this way, the hydrocarbonaceous material can retain a significant void volume between particles without substantial further crushing or compaction despite some small degree of compaction which often results from lithostatic pressure as the permeable body is formed.\|[0056] Once a desired permeable body has been formed within the control infrastructure, heat can be introduced sufficient to begin removal of hydrocarbons, e.g. via pyrolysis. A suitable heat source can be thermally associated with the permeable body. Optimal operating temperatures within the permeable body can vary depending on the composition and desired products. However, as a general guideline, operating temperatures can range from about 200° F. to about 750° F. Temperature variations throughout the encapsulated volume can vary and may reach as high as 900° F. or more in some areas. In one embodiment, the operating temperature can be a relatively lower temperature to facilitate production of liquid product such as from about 200° F. to about 650° F. This heating step can be a roasting operation which results in beneficiation of the crushed ore of the permeable body. Further, one embodiment comprises controlling the temperature, pressure and other variables sufficient to produce predominantly, and in some cases substantially only, liquid product. Generally, products can include both liquid and gaseous products, while liquid products can require fewer processing steps such as scrubbers etc. The relatively high permeability of the permeable body allows for production of liquid hydrocarbon products and minimization of gaseous products, depending to some extent on the particular starting materials and operating conditions. In one embodiment, the recovery of hydrocarbon products can occur substantially in the absence of cracking within the permeable body.\|[0057] In one aspect, heat can be transferred to the permeable body via convection. Heated gases can be injected into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body. Heated gases can be produced by combustion of natural gas, hydrocarbon product, or any other suitable source. The heated gases can be imported from external sources or recovered from the process.\|[0058] Alternatively, or in combination with convective heating, a highly configurable approach can include embedding a plurality of conduits within the permeable body. The conduits can be configured for use as heating pipes, cooling pipes, heat transfer pipes, drainage pipes, or gas pipes. Further, the conduits can be dedicated to a single function or may serve multiple functions during operation of the infrastructure, i.e. heat transfer and drainage. The conduits can be formed of any suitable material, depending on the intended function. Non-limiting examples of suitable materials can include clay pipes, refractory cement pipes, refractory ECC pipes, poured in place pipes, metal pipes such as cast iron, stainless steel etc., polymer such as PVC, and the like. In one specific embodiment, all or at least a portion of the embedded conduits can comprise a degradable material. For example, non-galvanized 6″ cast iron pipes can be effectively used for single use embodiments and perform well over the useful life of the impoundment, typically less than about 2 years. Further, different portions of the plurality of conduits can be formed of different materials. Poured in place pipes can be especially useful for very large encapsulation volumes where pipe diameters exceed several feet. Such pipes can be formed using flexible wraps which retain a viscous fluid in an annular shape. For example, PVC pipes can be used as a portion of a form along with flexible wraps, where concrete or other viscous fluid is pumped into an annular space between the PVC and flexible wrap. Depending on the intended function, perforations or other apertures can be made in the conduits to allow fluids to flow between the conduits and the permeable body. Typical operating temperatures exceed the melting point of conventional polymer and resin pipes. In some embodiments, the conduits can be placed and oriented such that the conduits intentionally melt or otherwise degrade during operation of the infrastructure.\|[0059] The plurality of conduits can be readily oriented in any configuration, whether substantially horizontal, vertical, slanted, branched, or the like. At least a portion of the conduits can be oriented along predetermined pathways prior to embedding the conduits within the permeable body. The predetermined pathways can be designed to improve heat transfer, gas-liquid-solid contacting, maximize fluid delivery or removal from specific regions within the encapsulated volume, or the like. Further, at least a portion the conduits can be dedicated to heating of the permeable body. These heating conduits can be selectively perforated to allow heated gases or other fluids to convectively heat and mix throughout the permeable body. The perforations can be located and sized to optimize even and/or controlled heating throughout the permeable body. Alternatively, the heating conduits can form a closed loop such that heating gases or fluids are segregated from the permeable body. Thus, a “closed loop” does not necessarily require recirculation, rather isolation of heating fluid from the permeable body. In this manner, heating can be accomplished primarily or substantially only through thermal conduction across the conduit walls from the heating fluids into the permeable body. Heating in a closed loop allows for prevention of mass transfer between the heating fluid and permeable body and can reduce formation and/or extraction of gaseous hydrocarbon products.\|[0060] During the heating or roasting of the permeable body, localized areas of heat which exceed parent rock decomposition temperatures, often above about 900° F., can reduce yields and form carbon dioxide and undesirable contaminating compounds which can lead to leachates containing heavy metals, soluble organics and the like. The heating conduits can allow for substantial elimination of such localized hot spots while maintaining a vast majority of the permeable body within a desired temperature range. The degree of uniformity in temperature can be a balance of cost (e.g. for additional heating conduits) versus yields. However, at least about 85% of the permeable body can readily be maintained within about 5-10% of a target temperature range with substantially no hot spots, i.e. exceeding the decomposition temperature of the hydrocarbonaceous materials such as about 800° F. and in many cases about 900° F. Thus, operated as described herein, the systems can allow for recovery of hydrocarbons while eliminating or substantially avoiding production of undesirable leachates. Although products can vary considerably depending on the starting materials, high quality liquid and gaseous products are possible. In accordance with one embodiment, a crushed oil shale material can produce a liquid product having an API from about 30 to about 45, with about 33 to about 38 being currently typical, directly from the oil shale without additional treatment. Interestingly, practice of these principles has led to an understanding that pressure appears to be a much less influential factor on the quality of recovered hydrocarbons than temperature and heating times. Although heating times can vary considerably, depending on void space, permeable body composition, quality, etc., as a general guideline times can range from a few days (i.e. 3-4 days) up to about one year. In one specific example, heating times can range from about 2 weeks to about 4 months. Under-heating oil shale at short residence times, i.e. minutes to several hours, can lead to formation of leachable and/or somewhat volatile hydrocarbons. Accordingly, these systems and processes allow for extended residence times at moderate temperatures such that organics present in oil shale can be volatilized and/or carbonized, leaving insubstantial leachable organics. In addition, the underlying shale is not generally decomposed or altered which reduces soluble salt formation.\|[0061] Further, conduits can be oriented among a plurality of impoundments and/or control infrastructures to transfer fluids and/or heat between the structures. The conduits can be welded to one another using conventional welding or the like. Further, the conduits can include junctions which allow for rotation and or small amounts of movement during expansion and subsidence of material in the permeable body. Additionally, the conduits can include a support system which acts to support the assembly of conduits prior to and during filling of the encapsulated volume, as well as during operation. For example, during heating flows of fluids, heating and the like can cause expansion (fracturing or popcorn effect) or subsidence sufficient to create potentially damaging stress and strain on the conduits and associated junctions. A truss support system or other similar anchoring members can be useful in reducing damage to the conduits. The anchoring members can include cement blocks, 1-beams, rebar, columns, etc. which can be associated with walls of the impoundment, including side walls, floors and ceilings.\|[0062] Alternatively, the conduits can be completely constructed and assembled prior to introduction of any mined materials into the encapsulated volume. Care and planning can be considered in designing the predetermined pathways of the conduits and method of filling the volume in order to prevent damage to the conduits during the filling process as the conduits are buried. Thus, as a general rule, the conduits used are oriented ab initio, or prior to embedding in the permeable body such that they are non-drilled. As a result, construction of the conduits and placement thereof can be performed without extensive core drilling and/or complicated machinery associated with well-bore or horizontal drilling. Rather, horizontal or any other orientation of conduit can be readily achieved by assembling the desired predetermined pathways prior to, or contemporaneous with, filling the infrastructure with the mined hydrocarbonaceous material. The non-drilled, hand/crane-placed conduits oriented in various geometric patterns can be laid with valve controlled connecting points which yield precise and closely monitored heating within the capsule impoundment. The ability to place and layer conduits including connecting, bypass and flow valves, and direct injection and exit points, allow for precision temperature and heating rates, precision pressure and pressurization rates, and precision fluid and gas ingress, egress and composition admixtures. For example, when a bacteria, enzyme, or other biological material is used, optimal temperatures can be readily maintained throughout the permeable body to increase performance, reaction, and reliability of such biomaterials.\|[0063] The conduits will generally pass through walls of the constructed infrastructure at various points. Due to temperature differences and tolerances, it can be beneficial to include an insulating material at the interface between the wall and the conduits. The dimensions of this interface can be minimized while also allowing space for thermal expansion differences during startup, steady-state operation, fluctuating operating conditions, and shutdown of the infrastructure. The interface can also involve insulating materials and sealant devices which prevent uncontrolled egress of hydrocarbons or other materials from the control infrastructure. Non-limiting examples of suitable materials can include high temperature gaskets, metal alloys, ceramics, clay or mineral liners, composites or other materials which having melting points above typical operating temperatures and act as a continuation of the permeability control provided by walls of the control infrastructure.\|[0064] Further, walls of the constructed infrastructure can be configured to minimize heat loss. In one aspect, the walls can be constructed having a substantially uniform thickness which is optimized to provide sufficient mechanical strength while also minimizing the volume of wall material through which the conduits pass. Specifically, excessively thick walls can reduce the amount of heat which is transferred into the permeable body by absorbing the same through conduction. Conversely, the walls can also act as a thermal barrier to somewhat insulate the permeable body and retain heat therein during operation.\|[0065] In one embodiment, fluid and gas compounds within the permeable body can be altered for desired extractive products using, as an example, induced pressure through gases or piled lithostatic pressure from piled rubble. Thus, some degree of upgrading and/or modification can be accomplished simultaneous with the recovery process. Further, certain hydrocarbonaceous materials can require treatment using specific diluents or other materials. For example, treatment of tar sands can be readily accomplished by steam injection or solvent injection to facilitate separation of bitumen from sand particles according to well known mechanisms.\|[0066] With the above description in mind, FIG. 1 depicts a side view of one embodiment showing an engineered capsule containment and extraction impoundment 100 where existing grade 108 is used primarily as support for the impermeable floor layer 112. Exterior capsule impoundment side walls 102 provide containment and can, but need not be, subdivided by interior walls 104. Subdividing can create separate containment capsules 122 within a greater capsule containment of the impoundment 100 which can be any geometry, size or subdivision. Further subdivisions can be horizontally or vertically stacked. By creating separate containment capsules 122 or chambers, classification of lower grade materials, varied gases, varied liquids, varied process stages, varied enzymes or microbiology types, or other desired and staged processes can be readily accommodated. Sectioned capsules constructed as silos within larger constructed capsules can also be designed to provide staged and sequenced processing, temperatures, gas and fluid compositions and thermal transfers. Such sectioned capsules can provide additional environmental monitoring and can be built of lined and engineered tailings berms similar to the primary exterior walls. In one embodiment, sections within the impoundment 100 can be used to place materials in isolation, in the absence of external heat, or with the intent of limited or controlled combustion or solvent application. Lower content hydrocarbon bearing material can be useful as a combustion material or as fill or a berm wall building material. Material which does not meet a various cut-off grade thresholds can also be sequestered without alteration in an impoundment dedicated for such purpose. In such embodiments, such areas may be completely isolated or bypassed by heat, solvents, gases, liquids, or the like. Optional monitoring devices and/or equipment can be permanently or temporarily installed within the impoundment or outside perimeters of the impoundments in order to verify containment of the sequestered material.\|[0067] Walls 102 and 104 as well as cap 116 and impermeable layer 112 can be engineered and reinforced by gabions 146 and or geogrid 148 layered in fill compaction. Alternatively, these walls 102, 104, 116 and 112 which comprise the permeability control impoundment and collectively define the encapsulated volume can be formed of any other suitable material as previously described. In this embodiment, the impoundment 100 includes side walls 102 and 104 which are self-supporting. In one embodiment, tailings berms, walls, and floors can be compacted and engineered for structure as well as permeability. The use of compacted geogrids and other deadman structures for support of berms and embankments can be included prior to or incorporated with permeability control layers which may include sand, clay, bentonite clay, gravel, cement, grout, reinforced cement, refractory cements, insulations, geo-membranes, drainpipes, temperature resistant insulations of penetrating heated pipes, etc.\|[0068] In one alternative embodiment, the permeability control impoundment can include side walls which are compacted earth and/or undisturbed geological formations while the cap and floors are impermeable. Specifically, in such embodiments an impermeable cap can be used to prevent uncontrolled escape of volatiles and gases from the impoundment such that appropriate gas collection outlets can be used. Similarly, an impermeable floor can be used to contain and direct collected liquids to a suitable outlet such the drain system 133 to remove liquid products from lower regions of the impoundment. Although impermeable side walls can be desirable in some embodiments, such are not always required. In some cases, side walls can be exposed undisturbed earth or compacted fill or earth, or other permeable material. Having permeable side walls may allow some small egress of gases and/or liquids from the impoundment.\|[0069] However, it may be desirable to have the impoundment constructed such that a positive pressure is maintained therein thereby preventing the introduction of air or other oxidizing gases from entering into the impoundment. The presence of oxygen can result in polymerization and gumming of the hydrocarbons and other contents within the impoundment. Further, the presence of oxygen can induce combustion within the system.\|[0070] Although not shown, above, below, around and adjacent to constructed capsule containment vessels environmental hydrology measures can be engineered to redirect surface water away from the capsule walls, floors, caps, etc. during operation. Further, gravity assisted drainage pipes and mechanisms can be utilized to aggregate and channel fluids, liquids or solvents within the encapsulated volume to central gathering, pumping, condensing, heating, staging and discharge pipes, silos, tanks, and/or wells as needed. In a similar manner, steam and/or water which is intentionally introduce, e.g. for tar sands bitumen treatment, can be recycled.\|[0071] Once wall structures 102 and 104 have been constructed above a constructed and impermeable floor layer 112 which commences from ground surface 106, the mined rubble 120 (which may be crushed or classified according to size or hydrocarbon richness), can be placed in layers upon (or next to) placed tubular heating pipes 118, fluid drainage pipes 124, and, or gas gathering or injection pipes 126. These pipes can be oriented and designed in any optimal flow pattern, angle, length, size, volume, intersection, grid, wall sizing, alloy construction, perforation design, injection rate, and extraction rate. In some cases, pipes such as those used for heat transfer can be connected to, recycled through or derive heat from heat source 134. Alternatively, or in combination with, recovered gases can be condensed by a condenser 140. Heat recovered by the condenser can be optionally used to supplement heating of the permeable body or for other process needs.\|[0072] Heat source 134 can derive, amplify, gather, create, combine, separate, transmit or include heat derived from any suitable heat source including, but not limited to, fuel cells (e.g. solid oxide fuel cells, molten carbonate fuel cells and the like), solar sources, wind sources, hydrocarbon liquid or gas combustion heaters, geothermal heat sources, nuclear power plant, coal fired power plant, radio frequency generated heat, wave energy, flameless combustors, natural distributed combustors, or any combination thereof. In some cases, electrical resistive heaters or other heaters can be used, although fuel cells and combustion-based heaters are particularly effective. In some locations, geothermal water can be circulated to the surface in adequate amounts to heat the permeable body and directed into the infrastructure.\|[0073] In another embodiment, electrically conductive material can be distributed throughout the permeable body and an electric current can be passed through the conductive material sufficient to generate heat. The electrically conductive material can include, but is not limited to, metal pieces or beads, conductive cement, metal coated particles, metal-ceramic composites, conductive semi-metal carbides, calcined petroleum coke, laid wire, combinations of these materials, and the like. The electrically conductive material can be premixed having various mesh sizes or the materials can be introduced into the permeable body subsequent to formation of the permeable body.\|[0074] Liquids or gases can transfer heat from heat source 134, or in another embodiment, in the cases of hydrocarbon liquid or gas combustion, radio frequency generators (microwaves), or fuel cells all can, but need not, actually generate heat inside of capsule impoundment area 114 or 122. In one embodiment, heating of the permeable body can be accomplished by convective heating from hydrocarbon combustion. Of particular interest is hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen. Stoichiometric conditions can allow for significantly increased heat gas temperatures. Stoichiometric combustion can employ but does not generally require a pure oxygen source which can be provided by known technologies including, but not limited to, oxygen concentrators, membranes, electrolysis, and the like. In some embodiments oxygen can be provided from air with stoichiometric amounts of oxygen and hydrogen. Combustion off gas can be directed to an ultra-high temperature heat exchanger, e.g. a ceramic or other suitable material having an operating temperature above about 2500° F. Air obtained from ambient or recycled from other processes can be heated via the ultra high temperature heat exchanger and then sent to the impoundment for heating of the permeable body. The combustion off gases can then be sequestered without the need for further separation, i.e. because the off gas is predominantly carbon dioxide and water.\|[0075] In order to minimize heat losses, distances can be minimized between the combustion chamber, heat exchanger and impoundments. Therefore, in one specific detailed embodiment portable combustors can be attached to individual heating conduits or smaller sections of conduits. Portable combustors or burners can individually provide from about 100,000 Btu to about 1,000,000 Btu with about 600,000 Btu per pipe generally being sufficient.\|[0076] Alternatively, in-capsule combustion can be initiated inside of isolated capsules within a primary constructed capsule containment structure. This process partially combusts hydrocarbonaceous material to provide heat and intrinsic pyrolysis. Unwanted air emissions 144 can be captured and sequestered in a formation 108 once derived from capsule containment 114, 122 or from heat source 134 and delivered by a drilled well bore 142. Heat source 134 can also create electricity and transmit, transform or power via electrical transmission lines 150. The liquids or gases extracted from capsule impoundment treatment area 114 or 122 can be stored in a nearby holding tank 136 or within a capsule containment 114 or 122. For example, the impermeable floor layer 112 can include a sloped area 110 which directs liquids towards drain system 133 where liquids are directed to the holding tank.\|[0077] As rubble material 120 is placed with piping 118, 124, 126, and 128, various measurement devices or sensors 130 are envisioned to monitor temperature, pressure, fluids, gases, compositions, heating rates, density, and all other process attributes during the extractive process within, around, or underneath the engineered capsule containment impoundment 100. Such monitoring devices and sensors 130 can be distributed anywhere within, around, part of, connected to, or on top of placed piping 118, 124, 126, and 128 or, on top of, covered by, or buried within rubble material 120 or impermeable barrier zone 112.\|[0078] As placed rubble material 120 fills the capsule treatment area 114 or 122, 120 becomes the ceiling support for engineered impermeable cap barrier zone 138, and wall barrier construction 170, which may include any combination of impermeability and engineered fluid and gas barrier or constructed capsule construction comprising those which may make up 112 including, but not limited to clay 162, compacted fill or import material 164, cement or refractory cement containing material 166, geo synthetic membrane, liner or insulation 168. Above 138, fill material can be oriented as ceiling cap 116 is placed to create lithostatic pressure upon the capsule treatment areas 114 or 122. Covering the permeable body with compacted fill sufficient to create an increased lithostatic pressure within the permeable body can be useful in further increasing hydrocarbon product quality. A compacted fill ceiling can substantially cover the permeable body, while the permeable body in return can substantially support the compacted fill ceiling. The compacted fill ceiling can further be sufficiently impermeable to removed hydrocarbon or an additional layer of permeability control material can be added in a similar manner as side and/or floor walls. Additional pressure can be introduced into extraction capsule treatment area 114 or 122 by increasing any gas or fluid once extracted, treated or recycled, as the case may be, via any of piping 118, 124, 126, or 128. In one embodiment the additional pressure is sufficient to maintain a positive pressure within the treatment area and is provided by the introduction of a non-oxidizing gas such as hydrogen, nitrogen, propane, carbon dioxide or any other gas which provides an inert atmosphere within the treatment area. Other potential flushing gases can include but are not limited to hydrocarbon gases. All relative measurements, optimization rates, injection rates, extraction rates, temperatures, heating rates, flow rates, pressure rates, capacity indicators, chemical compositions, or other data relative to the process of heating, extraction, stabilization, sequestration, impoundment, upgrading, refining or structure analysis within the capsule impoundment 100 are envisioned through connection to a computing device 132 which operates computer software for the management, calculation and optimization of the entire process. Further, core drilling, geological reserve analysis and assay modeling of a formation prior to blasting, mining and hauling (or at any time before, after or during such tasks) can serve as data input feeds into computer controlled mechanisms that operate software to identify optimal placements, dimensions, volumes and designs calibrated and cross referenced to desired production rate, pressure, temperature, heat input rates, gas weight percentages, gas injection compositions, heat capacity, permeability, porosity, chemical and mineral composition, compaction, density. Such analysis and determinations may include other factors like weather data factors such as temperature and air moisture content impacting the overall performance of the constructed infrastructure. Other data such as ore moisture content, hydrocarbon richness, weight, mesh size, and mineral and geological composition can be utilized as inputs including time value of money data sets yielding project cash flows, debt service and internal rates of return.\|[0079] FIG. 2A shows a collection of impoundments including an uncovered or uncapped capsule impoundment 100, containing sectioned capsule impoundments 122 inside of a mining quarry 200 with various elevations of bench mining. FIG. 2B illustrates a single impoundment 122 without associated conduits and other aspects merely for clarity. This impoundment can be similar to that illustrated in FIG. 1 or any other configuration. In some embodiments, it is envisioned that mining rubble can be transferred down chutes 230 or via conveyors 232 to the quarry capsule impoundments 100 and 122 without any need of mining haul trucks.\|[0080] FIG. 3 shows the engineered permeability barriers 112 below capsule impoundment 100 resting on exiting grade 106 of formation 108 with cap covering material or fill 302 on the sides and top of capsule impoundment 100 to ultimately (following the process) cover and reclaim a new earth surface 300. Indigenous plants which may have been temporarily moved from the area may be replanted such as trees 306. The constructed infrastructures can generally be single use structures which can be readily and securely shut down with minimal additional remediation. This can dramatically reduce costs associated with moving large volumes of spent materials. However, in some circumstances the constructed infrastructures can be excavated and reused. Some equipment such as radio frequency (RF) mechanisms, tubulars, devices and emitters may be recovered from within the constructed impoundment upon completion of hydrocarbon recovery.\|[0081] FIG. 4 shows computer means 130 controlling various property inputs and outputs of conduits 118, 126, or 128 connected to heat source 134 during the process among the subdivided impoundments 122 within a collective impoundment 100 to control heating of the permeable body. Similarly, liquid and vapor collected from the impoundments can be monitored and collected in tank 136 and condenser 140, respectively. Condensed liquids from the condenser can be collected in tank 141, while non-condensable vapor collected at unit 143. As described previously, the liquid and vapor products can be combined or more often left as separate products depending on condensability, target product, and the like. A portion of the vapor product can be optionally condensed and combined with the liquid products in tank 136. However, much of the vapor product will be C4 and lighter gases which can be burned, sold or used within the process. For example, hydrogen gas may be recovered using conventional gas separation and used to hydrotreat the liquid products according to conventional upgrading methods, e.g. catalytic, etc. or the non-condensable gaseous product can be burned to produce heat for use in heating the permeable body, heating an adjacent or nearby impoundment, heating service or personnel areas, or satisfying other process heat requirements. The constructed infrastructure can include thermocouples, pressure meters, flow meters, fluid dispersion sensors, richness sensors and any other conventional process control devices distributed throughout the constructed infrastructure. These devices can be each operatively associated with a computer such that heating rates, product flow rates, and pressures can be monitored or altered during heating of the permeable body. Optionally, in-place agitation can be performed using, for example, ultrasonic generators which are associated with the permeable body. Such agitation can facilitate separation and pyrolysis of hydrocarbons from the underlying solid materials with which they are associated. Further, sufficient agitation can reduce clogging and agglomeration throughout the permeable body and the conduits.\|[0082] FIG. 5 shows how any of the conduits can be used to transfer heat in any form of gas, liquid or heat via transfer means 510 from any sectioned capsule impoundment to another. Then, cooled fluid can be conveyed via heat transfer means 512 to the heat originating capsule 500, or heat originating source 134 to pick up more heat from capsule 500 to be again recirculated to a destination capsule 522. Thus, various conduits can be used to transfer heat from one impoundment to another in order to recycle heat and manage energy usage to minimize energy losses.\|[0083] In yet another aspect, a hydrogen donor agent can be introduced into the permeable body during the step of heating. The hydrogen donor agent can be any composition which is capable of hydrogenation of the hydrocarbons and can optionally be a reducing agent. Non-limiting examples of suitable hydrogen donor agents can include synthesis gas, propane, methane, hydrogen, natural gas, natural gas condensate, industrial solvents such as acetones, toluenes, benzenes, xylenes, cumenes, cyclopentanes, cyclohexanes, lower alkenes (C4-C10), terpenes, substituted compounds of these solvents, etc., and the like. Further, the recovered hydrocarbons can be subjected to hydrotreating either within the permeable body or subsequent to collection. Advantageously, hydrogen recovered from the gas products can be reintroduced into the liquid product for upgrading. Regardless, hydrotreating or hydrodesulfurization can be very useful in reducing nitrogen and sulfur content in final hydrocarbon products. Optionally, catalysts can be introduced to facilitate such reactions. In addition, introduction of light hydrocarbons into the permeable body can result in reforming reactions which reduce the molecular weight, while increasing the hydrogen to carbon ratio. This is particularly advantageous due at least in part to high permeability of the permeable body, e.g. often around 30%-40% void volume although void volume can generally vary from about 10% to about 50% void volume. Light hydrocarbons which can be injected can be any which provide reforming to recovered hydrocarbons. Non-limiting examples of suitable light hydrocarbons include natural gas, natural gas condensates, industrial solvents, hydrogen donor agents, and other hydrocarbons having ten or fewer carbons, and often five or fewer carbons. Currently, natural gas is an effective, convenient and plentiful light hydrocarbon. As mentioned previously, various solvents or other additives can also be added to aid in extraction of hydrocarbon products from the oil shale and can often also increase fluidity.\|[0084] The light hydrocarbon can be introduced into the permeable body by conveying the same through a delivery conduit having an open end in fluid communication with a lower portion of the permeable body such that the light hydrocarbons (which are a gas under normal operating conditions) permeate up through the permeable body. Alternatively, this same approach can be applied to recovered hydrocarbons which are first delivered to an empty impoundment. In this way, the impoundment can act as a holding tank for direct products from a nearby impoundment and as a reformer or upgrader. In this embodiment, the impoundment can be at least partially filled with a liquid product where the gaseous light hydrocarbon is passed through and allowed to contact the liquid hydrocarbon products at temperatures and conditions sufficient to achieve reforming in accordance with well known processes. Optional reforming catalysts which include metals such as Pd, Ni or other suitable catalytically active metals can also be included in the liquid product within the impoundment. The addition of catalysts can serve to lower and/or adjust reforming temperature and/or pressure for particular liquid products. Further, the impoundments can be readily formed at almost any depth. Thus, optimal reforming pressures (or recovery pressures when using impoundment depth as pressure control measure for recovery from a permeable body) can be designed based on hydrostatic pressure due to the amount of liquid in the impoundment and the height of the impoundment, i.e. P=ρgh. In addition, the pressure can vary considerably over the height of the impoundment sufficient to provide multiple reforming zones and tailorable pressures. Generally, pressures within the permeable body can be sufficient to achieve substantially only liquid extraction, although some minor volumes of vapor may be produced depending on the particular composition of the permeable body. As a general guideline, pressures can range from about 5 atm to about 50 atm, although pressures from about 6 atm to about 20 atm can be particularly useful. However, any pressure greater than about atmospheric can be used.\|[0085] In certain instances the maintaining of a positive pressure within the enclosed capsule, relative to the outside atmosphere, has certain advantages. For example, a positive pressure prevents unwanted gases from entering into the impoundment during the hydrocarbon removal process and further expedites the removal of hydrocarbons from within the impoundment. Maintaining a positive pressure by means of a non-oxidizing gas reduces the likelihood of unwanted combustion and retards or prevents polymerization of lighter hydrocarbons which can form deposits on pipes or other infrastructure within the impoundment. Also, a positive pressure enables the flushing of the system in the event of certain events or happenings. One example might be in the event there is an interruption of the processing of the hydrocarbonaceous material and the collection of hydrocarbons due to a leak or other unwanted escape of fluids from within the impoundment. A positive pressure allows for the almost instantaneous introduction of non-oxidizing gases at a predetermined temperature, preferably a cooling temperature, to flush hydrocarbons and other vaporous components from the permeable body and within the impoundment so as to maintain an inert environment until any problem is detected and corrected. As previously noted gases such as hydrogen, nitrogen, propane, carbon dioxide, hydrocarbons, and the like can be used to flush the impoundment. Although any functional positive pressure can be suitable, pressure can generally be from about 1.01 atm to about 10 atm, and in one aspect from about 1.1 atm to about 4 atm.\|[0086] Further, once the hydrocarbon production stage is completed, the impoundment can be flushed with a non-oxidizing gas in order to remove further recoverable hydrocarbons from the impoundment. Such flushing can be accomplished in stages or in increments of temperature reduction or any other means to recover meaningful quantities of hydrocarbons. It may be beneficial to allow such flushing and cooling in increments such as to maximize the recovery of hydrocarbons while, at the same time, prepare the hydrocarbon lean shale or other materials, for further processing and/or pacification. The flushing times will obviously depend on the size of the permeable body and the impoundment and can be accomplished in a matter of hours, days or even weeks.\|[0087] Also, the lean shale or other inorganic matter resulting from the termination of the hydrocarbon removal process may still contain other components such as heavy metals, precious metals or other mineral components in the permeable body that can be extracted in further processing steps. Certain deposits may contain radioactive materials that require further processing and/or impounding in order to comply with governmental regulations.\|[0088] In one embodiment, extracted crude has fines precipitated out within the subdivided capsules. Extracted fluids and gases can be treated for the removal of fines and dust particles. Separation of fines from shale oil can be accomplished by techniques such as, but not limited to, hot gas filtering, precipitation, and heavy oil recycling.\|[0089] Hydrocarbon products recovered from the permeable body can be further processed (e.g. refined) or used as produced. Any condensable gaseous products can be condensed by cooling and collection, while non-condensable gases can be collected, burned as fuel, reinjected, or otherwise utilized or disposed of Optionally, mobile equipment can be used to collect gases. These units can be readily oriented proximate to the control infrastructure and the gaseous product directed thereto via suitable conduits from an upper region of the control infrastructure.\|[0090] In yet another alternative embodiment, heat within the permeable body can be recovered subsequent to primary recovery of hydrocarbon materials therefrom. For example, a large amount of heat is retained in the permeable body. In one optional embodiment, the permeable body can be flooded with a heat transfer fluid such as water to form a heated fluid, e.g. heated water and/or steam. At the same time, this process can facilitate removal of some residual hydrocarbon products via a physical rinsing of the spent shale solids. In some cases, the introduction of water and presence of steam can result in water gas shift reactions and formation of synthesis gas. Steam recovered from this process can be used to drive a generator, directed to another nearby infrastructure, or otherwise used. Hydrocarbons and/or synthesis gas can be separated from the steam or heated fluid by conventional methods.\|[0091] Although the methods and infrastructure allow for improved permeability and control of operating conditions, significant quantities of unrecovered hydrocarbons, precious metals, minerals, sodium bicarbonate or other commercially valuable materials often remain in the permeable body. Therefore, a selective solvent can be injected or introduced into the permeable body. Typically, this can be done subsequent to collecting the hydrocarbons, although certain selective solvents can be beneficially used prior to heating and/or collection. This can be done using one or more of the existing conduits or by direct injection and percolation through the permeable body. The selective solvent or leachate can be chosen as a solvent for one or more target materials, e.g. minerals, precious metal, heavy metals, hydrocarbons, or sodium bicarbonate. In one specific embodiment, steam or carbon dioxide can be used as a rinse of the permeable body to dislodge at least a portion of any remaining hydrocarbons. This can be beneficial not only in removing potentially valuable secondary products, but also in cleaning remaining spent materials of trace heavy metal or inorganics to below detectable levels in order to comply with regulatory standards or to prevent inadvertent leaching of materials at a future date.\|[0092] More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body. Typically, such recovery of materials can be performed prior to heat treatment of the permeable body. Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like. For example, heavy metals, bauxite or aluminum, and mercury can be removed by flooding the permeable body with an appropriate solvent and recirculating the resulting leachate through appropriately designed ion exchange resins (e.g. beads, membranes, etc.).\|[0093] Similarly, bioextraction, bio leaching, biorecovery, or bioremediation of hydrocarbon material, spent materials, or precious metals can be performed to further improve remediation, extract valuable metals, and restoration of spent material to environmentally acceptable standards. In such bioextraction scenarios, conduits can be used to inject catalyzing gases as a precursor which helps to encourage bioreaction and growth. Such microorganisms and enzymes can biochemically oxidize the ore body or material or cellulosic or other biomass material prior to an ore solvent extraction via bio-oxidation. For example, a perforated pipe or other mechanism can be used to inject a light hydrocarbon (e.g. methane, ethane, propane or butane) into the permeable body sufficient to stimulate growth and action of native bacteria. Bacteria can be native or introduced and may grow under aerobic or anaerobic conditions. Such bacteria can release metals from the permeable body which can then be recovered via flushing with a suitable solvent or other suitable recovery methods. The recovered metals can then be precipitated out using conventional methods.\|[0094] Synthesis gas can also be recovered from the permeable body during the step of heating. Various stages of gas production can be manipulated through processes which raise or lower operating temperatures within the encapsulated volume and adjust other inputs into the impoundment to produce synthetic gases which can include but are not limited to, carbon monoxide, hydrogen, hydrogen sulfide, hydrocarbons, ammonia, water, nitrogen or various combinations thereof. In one embodiment, temperature and pressure can be controlled within the permeable body to lower CO2 emissions as synthetic gases are extracted.\|[0095] Hydrocarbon product recovered from the constructed infrastructures can most often be further processed, e.g. by upgrading, refining, etc. Sulfur from related upgrading and refining processing can be isolated in various constructed sulfur capsules within the greater structured impoundment capsule. Constructed sulfur capsules can be spent constructed infrastructures or dedicated for the purpose of storage and isolation after desulfurization.\|[0096] Similarly, spent hydrocarbonaceous material remaining in the constructed infrastructure can be utilized in the production of cement and aggregate products for use in construction or stabilization of the infrastructure itself or in the formation of offsite constructed infrastructures. Such cement products made with the spent shale may include, but are not limited to, mixtures with Portland cement, calcium salt, volcanic ash, perlite, synthetic nano carbons, sand, fiber glass, crushed glass, asphalt, tar, binding resins, cellulosic plant fibers, and the like.\|[0097] In still another embodiment, injection, monitoring and production conduits or extraction egresses can be incorporated into any pattern or placement within the constructed infrastructure. Monitoring wells and constructed geo membrane layers beneath or outside of the constructed capsule containment can be employed to monitor unwanted fluid and moisture migration outside of containment boundaries and the constructed infrastructure.\|[0098] Although a filled and prepared constructed infrastructure can often be immediately heated to recover hydrocarbons, this is not required. For example, a constructed infrastructure which is built and filled with mined hydro carbonaceous material can be left in place as a proven reserve. Such structures are less susceptible to explosion or damage due to terrorist activity and can also provide strategic reserves of unprocessed petroleum products, with classified and known properties so that economic valuations can be increased and more predictable. Long term petroleum storage often faces quality deterioration issues over time. Thus, these approaches can optionally be used for long term quality insurance and storage with reduced concerns regarding breakdown and degradation of hydrocarbon products.\|[0099] In still another aspect, the high quality liquid product can be blended with more viscous lower quality (e.g. lower API) hydrocarbon products. For example, kerogen oil produced from the impoundments can be blended with bitumen to form a blended oil. The bitumen is typically not transportable through an extended pipeline under conventional and accepted pipeline standards and can have a viscosity substantially above and an API substantially below that of the kerogen oil. By blending the kerogen oil and bitumen, the blended oil can be rendered transportable without the use of additional diluents or other viscosity or API modifiers. As a result, the blended oil can be pumped through a pipeline without requiring additional treatments to remove a diluent or returning such diluents via a secondary pipeline. Conventionally, bitumen is combined with a diluent such as natural gas condensate or other low molecular weight liquids, to allow pumping to a remote location. The diluent is removed and returned via a second pipeline back to the bitumen source. These approaches allow for elimination of returning diluent and simultaneous upgrading of the bitumen.\|[0100] Although these processes are mining-dependent, they are not limited or encumbered to conventional aboveground (ex-situ) retorting processes. This approach improves upon the benefits of surface retorts including better process control of temperature, pressure, injection rates, fluid and gas compositions, product quality and better permeability due to processing and heating mined rubble. These advantages are available while still addressing the volume, handling, and scalability issues most fabricated surface retorts cannot provide.\|[0101] Other improvements which can be realized are related to environmental protection. Conventional surface retorts have had the problem of spent shale after it has been mined and has passed through a surface retort. Spent shale which has been thermally altered requires special handling to reclaim and isolate from surface drainage basins and underground aquifers. This approach addresses reclamation and retorting in a uniquely combined approach. In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants. This approach uniquely provides solutions to problems for not just one, but many problems, and in an integrated approach. As a result, significant benefits to the public can be achieved in terms of energy production, economic opportunity, environmental stewardship and energy output.\|[0102] It is to be understood that the above-referenced arrangements are illustrative of the application for the principles of the present invention. Thus, while the present invention has been described above in connection with the exemplary embodiments, it will be apparent to those of ordinary skill in the art that numerous modifications and alternative arrangements can be made without departing from the principles and concepts of the invention as set forth in the claims.	(US8349171)\|RELATED APPLICATION\|[0001] This application claims priority to U.S. Provisional Patent Application No. 61/152,146, filed Feb. 12, 2009, which is incorporated herein by reference.\|(US8349171)\|BACKGROUND\|[0002] Global and domestic demand for fossil fuels continues to rise despite price increases and other economic and geopolitical concerns. As such demand continues to rise, research and investigation into finding additional economically viable sources of fossil fuels correspondingly increases. Historically, many have recognized the vast quantities of energy stored in oil shale, coal and tar sand deposits, for example. However, these sources remain a difficult challenge in terms of economically competitive recovery. Canadian tar sands have shown that such efforts can be fruitful, although many challenges still remain, including environmental impact, product quality, production costs and process time, among others.\|[0003] Estimates of world-wide oil shale reserves range from two to almost seven trillion barrels of oil, depending on the estimating source. Regardless, these reserves represent a tremendous volume and remain a substantially untapped resource. A large number of companies and investigators continue to study and test methods of recovering oil from such reserves. In the oil shale industry, methods of extraction have included underground rubble chimneys created by explosions, in-situ methods such as In-Situ Conversion Process (ICP) method (Shell Oil), and heating within steel fabricated retorts. Other methods have included in-situ radio frequency methods (microwaves), and “modified” in-situ processes wherein underground mining, blasting and retorting have been combined to make rubble out of a formation to allow for better heat transfer and product removal.\|[0004] Among typical oil shale processes, all face tradeoffs in economics and environmental concerns. No current process alone satisfies economic, environmental and technical challenges. Moreover, global warming concerns give rise to additional measures to address carbon dioxide (CO2) emissions which are associated with such processes. Methods are needed that accomplish environmental stewardship, yet still provide high-volume cost-effective oil production.\|[0005] Below ground in-situ concepts emerged based on their ability to produce high volumes while avoiding the cost of mining. While the cost savings resulting from avoiding mining can be achieved, the in-situ method requires heating a formation for a longer period of time due to the extremely low thermal conductivity and high specific heat of solid oil shale. Perhaps the most significant challenge for any in-situ process is the uncertainty and long term potential of water contamination that can occur with underground freshwater aquifers. In the case of Shell's ICP method, a “freeze wall” is used as a barrier to keep separation between aquifers and an underground treatment area. Although this is possible, no long term analysis has proven for extended periods to guarantee the prevention of contamination. Without guarantees and with even fewer remedies should a freeze wall fail, other methods are desirable to address such environmental risks.\|[0006] For this and other reasons, the need remains for methods and systems which can provide improved recovery of hydrocarbons from suitable hydrocarbon-containing materials, which have acceptable economics and avoid the drawbacks mentioned above.\|SUMMARY\|[0007] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating the hydrocarbonaceous material can be substantially stationary. Removed fluid hydrocarbons can be collected for further processing, use in the process as supplemental fuel or additives, and/or direct use without further treatment.\|[0008] These systems and processes can allow difficult problems to be solved related to the extraction of hydrocarbon liquids and gases from surface or underground mined hydrocarbon bearing deposits such as oil shale, tar sands, lignite, and coal, and from harvested biomass. Among other things, this approach helps reduce cost, increase volume output, lower air emissions, limit water consumption, prevent underground aquifer contamination, reclaim surface disturbances, reduce material handling costs, remove dirty fine particulates, and improve composition of recovered hydrocarbon liquid or gas. It also addresses water contamination issues with a safer, more predictable, engineered, observable, repairable, adaptable and preventable water protection structure.\|[0009] Additional features and advantages of the invention will be apparent from the following detailed description, which illustrates, by way of example, features of the invention.\|(US8349171)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0010] FIG. 1 is side partial cutaway view schematic of a constructed permeability control infrastructure in accordance with one embodiment.\|[0011] FIGS. 2A and 2B are top and plan views of a plurality of permeability control impoundments in accordance with one embodiment.\|[0012] FIG. 3 is a side cutaway view of a permeability control impoundment in accordance with one embodiment.\|[0013] FIG. 4 is a schematic of a portion of a constructed infrastructure in accordance with an embodiment.\|[0014] FIG. 5 is a schematic showing heat transfer between two permeability control impoundments in accordance with another embodiment.\|(US8349171)\|DETAILED DESCRIPTION\|[0015] It should be noted that the figures are merely exemplary of several embodiments and no limitations on the scope of the present invention are intended thereby. Further, the figures are generally not drawn to scale, but are drafted for purposes of convenience and clarity in illustrating various aspects of the invention.\|DETAILED DESCRIPTION\|[0016] Reference will now be made to exemplary embodiments and specific language will be used herein to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended. Alterations and further modifications of the inventive features described herein, and additional applications of the principles of the invention as described herein, which would occur to one skilled in the relevant art and having possession of this disclosure, are to be considered within the scope of the invention. Further, before particular embodiments are disclosed and described, it is to be understood that this invention is not limited to the particular process and materials disclosed herein as such may vary to some degree. It is also to be understood that the terminology used herein is used for the purpose of describing particular embodiments only and is not intended to be limiting, as the scope of the present invention will be defined only by the appended claims and equivalents thereof.\|DEFINITIONS\|[0017] In describing and claiming the present invention, the following terminology will be used.\|[0018] The singular forms “a,” “an,” and “the” include plural references unless the context clearly dictates otherwise. Thus, for example, reference to “a wall” includes reference to one or more of such structures, “a permeable body” includes reference to one or more of such materials, and “a heating step” refers to one or more of such steps.\|[0019] As used herein “existing grade” or similar terminology refers to the grade or a plane parallel to the local surface topography of a site containing an infrastructure as described herein which infrastructure may be above or below the existing grade.\|[0020] As used herein, “conduits” refers to any passageway along a specified distance which can be used to transport materials and/or heat from one point to another point. Although conduits can generally be circular pipes, other non-circular conduits can also be useful. Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|[0021] As used herein, “constructed infrastructure” refers to a structure which is substantially entirely man made, as opposed to freeze walls, sulfur walls, or other barriers which are formed by modification or filling pores of an existing geological formation.\|[0022] The constructed permeability control infrastructure is often substantially free of undisturbed geological formations, although the infrastructure can be formed adjacent or in direct contact with an undisturbed formation. Such a control infrastructure can be unattached or affixed to an undisturbed formation by mechanical means, chemical means or a combination of such means, e.g. bolted into the formation using anchors, ties, or other suitable hardware.\|[0023] As used herein, “comminuted” refers to breaking a formation or larger mass into pieces. A comminuted mass can be rubbilized or otherwise broken into fragments.\|[0024] As used herein, “hydrocarbonaceous material” refers to any hydrocarbon-containing material from which hydrocarbon products can be extracted or derived. For example, hydrocarbons may be extracted directly as a liquid, removed via solvent extraction, directly vaporized or otherwise removed from the material. However, many hydrocarbonaceous materials contain kerogen or bitumen which is converted to a hydrocarbon through heating and pyrolysis. Hydrocarbonaceous materials can include, but is not limited to, oil shale, tar sands, coal, lignite, bitumen, peat, and other organic materials.\|[0025] As used herein, “impoundment” refers to a structure designed to hold or retain an accumulation of fluid and/or solid moveable materials. An impoundment generally derives at least a substantial portion of foundation and structural support from earthen materials. Thus, the control walls do not always have independent strength or structural integrity apart from the earthen material and/or formation against which they are formed.\|[0026] As used herein, “permeable body” refers to any mass of comminuted hydrocarbonaceous material having a relatively high permeability which exceeds permeability of a solid undisturbed formation of the same composition. Suitable permeable bodies can have greater than about 10% void space and typically have void space from about 30% to 45%, although other ranges may be suitable. Allowing for high permeability facilitates, for example, through the incorporation of large irregularly shaped particles, heating of the body through convection as the primary heat transfer while also substantially reducing costs associated with crushing to very small sizes, e.g. below about 1 to about 0.5 inch.\|[0027] As used herein, “wall” refers to any constructed feature having a permeability control contribution to confining material within an encapsulated volume defined at least in part by control walls. Walls can be oriented in any manner such as vertical, although ceilings, floors and other contours defining the encapsulated volume can also be “walls” as used herein.\|[0028] As used herein, “mined” refers to a material which has been removed or disturbed from an original stratographic or geological location to a second and different location or returned to the same location. Typically, mined material can be produced by rubbilizing, crushing, explosively detonating, or otherwise removing material from a geologic formation.\|[0029] As used herein, “substantially stationary” refers to nearly stationary positioning of materials with a degree of allowance for subsidence, expansion, and/or settling as hydrocarbons are removed from the hydrocarbonaceous material from within the enclosed volume to leave behind lean material. In contrast, any circulation and/or flow of hydrocarbonaceous material such as that found in fluidized beds or rotating retorts involves highly substantial movement and handling of hydro carbonaceous material.\|[0030] As used herein, “substantial” when used in reference to a quantity or amount of a material, or a specific characteristic thereof, refers to an amount that is sufficient to provide an effect that the material or characteristic was intended to provide. The exact degree of deviation allowable may in some cases depend on the specific context. Similarly, “substantially free of” or the like refers to the lack of an identified element or agent in a composition. Particularly, elements that are identified as being “substantially free of” are either completely absent from the composition, or are included only in amounts which are small enough so as to have no measurable effect on the composition.\|[0031] As used herein, “about” refers to a degree of deviation based on experimental error typical for the particular property identified. The latitude provided the term “about” will depend on the specific context and particular property and can be readily discerned by those skilled in the art. The term “about” is not intended to either expand or limit the degree of equivalents which may otherwise be afforded a particular value. Further, unless otherwise stated, the term “about” shall expressly include “exactly,” consistent with the discussion below regarding ranges and numerical data.\|[0032] Concentrations, dimensions, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of about 1 to about 200 should be interpreted to include not only the explicitly recited limits of 1 and 200, but also to include individual sizes such as 2, 3, 4, and sub-ranges such as 10 to 50, 20 to 100, etc.\|[0033] As used herein, a plurality of items, structural elements, compositional elements, and/or materials may be presented in a common list for convenience. However, these lists should be construed as though each member of the list is individually identified as a separate and unique member. Thus, no individual member of such list should be construed as a de facto equivalent of any other member of the same list solely based on their presentation in a common group without indications to the contrary.\|[0034] Recovering Hydrocarbons from Hydrocarbonaceous Materials Under Positive Pressure\|[0035] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined or harvested hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure is a fixed structure. Removed fluid hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.\|[0036] The constructed permeability control infrastructure can be formed using existing grade as floor support and/or as side wall support for the constructed infrastructure. For example, the control infrastructure can be formed as a free standing structure, i.e. using only existing grade as a floor with side walls being man-made. Alternatively, the control infrastructure can be formed within an excavated pit.\|[0037] A constructed permeability control infrastructure can include a permeability control impoundment which defines a substantially encapsulated volume. The permeability control impoundment is substantially free of undisturbed geological formations. Specifically, the permeability control aspect of the impoundment can be completely constructed and manmade as a separate isolation mechanism for prevention of uncontrolled migration of material into or out of the encapsulated volume.\|[0038] In one embodiment, the permeability control impoundment can be formed along walls of an excavated hydrocarbonaceous material deposit. For example, oil shale, tar sands, or coal can be mined from a deposit to form a cavity which corresponds approximately to a desired encapsulation volume for an impoundment. The excavated cavity can then be used as a form and support to create the permeability control impoundment.\|[0039] In one alternative aspect, at least one additional excavated hydrocarbonaceous material deposit can be formed such that a plurality of impoundments can be operated. Further, such a configuration can facilitate a reduction in transportation distance of the mined material. Specifically, the mined hydrocarbonaceous material for any particular encapsulated volume can be mined from an adjacent excavated hydrocarbonaceous material deposit. In this manner, a grid of constructed structures can be built such that mined material can be immediately and directly filled into an adjacent impoundment.\|[0040] Mining and/or excavation of hydro carbonaceous deposits can be accomplished using any suitable technique. Conventional surface mining can be used, although alternative excavators can also be used without requirement of transportation of the mined materials. In one specific embodiment, the hydrocarbonaceous deposit can be excavated using a crane-suspended excavator. One example of a suitable excavator can include vertical tunnel boring machines. Such machines can be configured to excavate rock and material beneath the excavator. As material is removed, the excavator is lowered to ensure substantially continuous contact with a formation. Removed material can be conveyed out of the excavation area using conveyors or lifts. Alternatively, the excavation can occur under aqueous slurry conditions to reduce dust problems and act as a lubricant/coolant. The slurry material can be pumped out of the excavation for separation of solids in a settling tank or other similar solid-liquid separator, or the solids may be allowed to precipitate directly in an impoundment. This approach can be readily integrated with simultaneous or sequential solution-based recovery of metals and other materials as described in more detail below.\|[0041] Further, excavation and formation of a permeability control impoundment can be accomplished simultaneously. For example, an excavator can be configured to remove hydro carbonaceous material while side walls of an impoundment are formed. Material can be removed from just underneath edges of the side walls such that the walls can be guided downward to allow additional wall segments to be stacked above. This approach can allow for increased depths while avoiding or reducing dangers of cave-in prior to formation of supporting impoundment walls.\|[0042] The impoundment can be formed of any suitable material which provides isolation of material transfer across walls of the impoundment. In this manner, integrity of the walls is retained during operation of the control infrastructure sufficient to substantially prevent uncontrolled migration of fluids outside of the control infrastructure. Non-limiting examples of suitable material for use in forming the impoundment of the constructed permeability control infrastructure can include clay, bentonite clay (e.g. clay comprising at least a portion of bentonite), bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, or combinations thereof. Engineered cementitious composites (ECC) materials, fiber reinforced composites, and the like can be particularly strong and can be readily engineered to meet permeability and temperature tolerance requirements of a given installation. As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required. For example, materials having a melting point above the maximum operating temperature of the infrastructure can be useful to maintain containment during and after heating and recovery. However, lower temperature materials can also be used if a non-heated buffer zone is maintained between the walls and heated portions of the permeable body. Such buffer zones can range from 6 inches to 50 feet depending on the particular material used for the impoundment and the composition of the permeable body. In another aspect, walls of the impoundment can be acid, water and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water. For impoundment walls formed along formations or other solid support, the impoundment walls can be formed of a sprayed grouting, sprayed liquid emulsions, or other sprayed material such as sprayable refractory grade grouting which forms a seal against the formation and creates the permeability control wall of the impoundments. Impoundment walls may be substantially continuous such that the impoundment defines the encapsulated volume sufficiently to prevent substantial movement of fluids into or out of the impoundment other than defined inlets and outlets, e.g. via conduits or the like as discussed herein. In this manner, the impoundments can readily meet government fluid migration regulations. Alternatively, or in combination with a manufactured barrier, portions of the impoundment walls can be undisturbed geological formation and/or compacted earth. In such cases, the constructed permeability control infrastructure is a combination of permeable and impermeable walls as described in more detail below.\|[0043] In one detailed aspect, a portion of hydrocarbonaceous material, either pre- or post-processed, can be used as a cement fortification and/or cement base which are then poured in place to form portions or the entirety of walls of the control infrastructure. These materials can be formed in place or can be preformed and then assembled on site to form an integral impoundment structure. For example, the impoundment can be constructed by cast forming in place as a monolithic body, extrusion, stacking of preformed or precast pieces, concrete panels joined by a grout (cement, ECC or other suitable material), inflated form, or the like. The forms can be built up against a formation or can be stand alone structures. Forms can be constructed of any suitable material such as, but not limited to, steel, wood, fiberglass, polymer, or the like. The forms can be assembled in place or may be oriented using a crane or other suitable mechanism. Alternatively, the constructed permeability control infrastructure can be formed of gabions and/or geosynthetic fabrics assembled in layers with compacted fill material. Optional binders can be added to enhance compaction of the permeability control walls. In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|[0044] Impoundment walls can optionally include non-permeable insulation and/or fines collection layers. These permeable layers can be oriented between the permeability control barrier and the permeable body. For example, a layer of hydrocarbonaceous comminuted material can be provided which allows fluids to enter, cool, and at least partially condense within the layer. Such permeable layer material can generally have a particle size smaller than the permeable body. Further, such hydrocarbonaceous material can remove fines from passing fluids via various attractive forces. In one embodiment, the construction of impoundment walls and floors can include multiple compacted layers of indigenous or manipulated low grade shale with any combination of sand, cement, fiber, plant fiber, nano carbons, crushed glass, reinforcement steel, engineered carbon reinforcement grid, calcium salts, and the like. In addition to such composite walls, designs which inhibit long term fluid and gas migration through additional impermeability engineering can be employed including, but not limited to, liners, geo-membranes, compacted soils, imported sand, gravel or rock and gravity drainage contours to move fluids and gases away from impervious layers to egress exits. Impoundment floor and wall construction, can, but need not comprise, a stepped up or stepped down slope or bench as the case of mining course may dictate following the optimal ore grade mining. In any such stepped up or down applications, floor leveling and containment wall construction can typically drain or slope to one side or to a specific central gathering area(s) for removal of fluids by gravity drainage assistance.\|[0045] Optionally, capsule wall and floor construction can include insulation which prevents heat transfer outside of the constructed infrastructure or outside of inner capsules or conduits within the primary constructed capsule containment. Insulation can comprise manufactured materials, cement or various materials other materials which are less thermally conductive than surrounding masses, i.e. permeable body, formation, adjacent infrastructures, etc. Thermally insulating barriers can also be formed within the permeable body, along impoundment walls, ceilings and/or floors. One detailed aspect includes the use of biodegradable insulating materials, e.g. soy insulation and the like. This is consistent with embodiments wherein the impoundment is a single use system such that insulations, pipes, and/or other components can have a relatively low useful life, e.g. less than 1-2 years. This can reduce equipment costs as well as reduce long-term environmental impact.\|[0046] These structures and methods can be applied at almost any scale. Larger encapsulated volumes and increased numbers of impoundments can readily produce hydrocarbon products and performance comparable to or exceeding smaller constructed infrastructures. As an illustration, single impoundments can range in size from tens of meters across to tens of acres. Optimal impoundment sizes may vary depending on the hydrocarbonaceous material and operating parameters, however it is expected that suitable areas can range from about one-half to five acres in top plan surface area.\|[0047] The methods and infrastructures can be used for recovery of hydrocarbons from a variety of hydrocarbonaceous materials. One particular advantage is a wide degree of latitude in controlling particle size, conditions, and composition of the permeable body introduced into the encapsulated volume. Non-limiting examples of mined hydrocarbonaceous material which can be treated comprise oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof. In some cases it can be desirable to provide a single type of hydrocarbonaceous material so that the permeable body consists essentially of one of the above materials. However, the permeable body can include mixtures of these materials such that grade, oil content, hydrogen content, permeability and the like can be adjusted to achieve a desired result. Further, different hydrocarbon materials can be placed in multiple layers or in a mixed fashion such as combining coal, oil shale, tar sands, biomass, and/or peat.\|[0048] In one embodiment, hydrocarbon containing material can be classified into various inner capsules within a primary constructed infrastructure for optimization reasons. For instance, layers and depths of mined oil shale formations may be richer in certain depth pay zones as they are mined. Once, blasted, mined, shoveled and hauled inside of capsule for placement, richer oil bearing ores can be classified or mixed by richness for optimal yields, faster recovery, or for optimal averaging within each impoundment. Further, providing layers of differing composition can have added benefits. For example, a lower layer of tar sands can be oriented below an upper layer of oil shale. Generally, the upper and lower layers can be in direct contact with one another although this is not required. The upper layer can include heating pipes embedded therein as described in more detail below. The heating pipes can heat the oil shale sufficient to liberate kerogen oil, including short-chain liquid hydrocarbons, which can act as a solvent for bitumen removal from the tar sands. In this manner, the upper layer acts as an in situ solvent source for enhancing bitumen removal from the lower layer. Heating pipes within the lower layer are optional such that the lower layer can be free of heating pipes or may include heating pipes, depending on the amount of heat transferred via downward passing liquids from the upper layer and any other heat sources. The ability to selectively control the characteristics and composition of the permeable body adds a significant amount of freedom in optimizing oil yields and quality.\|[0049] Furthermore, in many embodiments, the liberated gaseous and liquid products act as an in situ produced solvent which supplements kerogen removal and/or additional hydrocarbon removal from the hydro carbonaceous material.\|[0050] In yet another detailed aspect, the permeable body can further comprise an additive or biomass. Additives can include any composition which acts to increase the quality of removed hydrocarbons, e.g. increased API, decreased viscosity, improved flow properties, reduced wetting of residual shale, reduction of sulfur, hydrogenation agents, etc. Non-limiting examples of suitable additives can include bitumen, kerogen, propane, natural gas, natural gas condensate, crude oil, refining bottoms, asphaltenes, common solvents, other diluents, and combinations of these materials. In one specific embodiment, the additive can include a flow improvement agent and/or a hydrogen donor agent. Some materials can act as both or either agents to improve flow or as a hydrogen donor. Non-limiting examples of such additives can include methane, natural gas condensates, common solvent such as acetone, toluene, benzene, etc., and other additives listed above. Additives can act to increase the hydrogen to carbon ratio in any hydrocarbon products, as well as act as a flow enhancement agent. For example, various solvents and other additives can create a physical mixture which has a reduced viscosity and/or reduced affinity for particulate solids, rock and the like. Further, some additives can chemically react with hydrocarbons and/or allow liquid flow of the hydrocarbon products. Any additives used can become part of a final recovered product or can be removed and reused or otherwise disposed of.\|[0051] Similarly, biological hydroxylation of hydrocarbonaceous materials to form synthetic gas or other lighter weight products can be accomplished using known additives and approaches. Enzymes or biocatalysts can also be used in a similar manner. Further, manmade materials can also be used as additives such as, but not limited to, tires, polymeric refuse, or other hydrocarbon-containing materials.\|[0052] Although these methods are broadly applicable, as a general guideline, the permeable body can include particles from about ⅛ inch to about 6 feet in largest dimension, and in some cases less than 1 foot and in other cases less than about 6 inches. However, as a practical matter, sizes from about 2 inches to about 2 feet can provide good results with about 1 foot diameter being useful for oil shale especially. Void space can be an important factor in determining optimal particle diameters. As a general matter, any functional void space can be used; however, about 10% to about 50% and in some cases about 30% to about 45% usually provides a good balance of permeability and effective use of available volumes. Void volumes can be varied somewhat by varying other parameters such as heating conduit placement, additives, and the like. Mechanical separation of mined hydrocarbonaceous materials allows creation of fine mesh, high permeability particles which enhance thermal dispersion rates once placed in capsule within the impoundment. The added permeability allows for more reasonable, low temperatures which also help to avoid higher temperatures which result in greater CO2 production from carbonate decomposition and associated release of trace heavy metals, volatile organics, and other compounds which can create toxic effluent and/or undesirable materials which can be monitored and controlled.\|[0053] In one embodiment, computer assisted mining, mine planning, hauling, blasting, assay, loading, transport, placement, and dust control measures can be utilized to fill and optimize the speed of mined material movement into the constructed capsule containment structure. In one alternative aspect, the impoundments can be formed in excavated volumes of a hydrocarbonaceous formation, although other locations remote from the control infrastructure can also be useful. For example, some hydrocarbonaceous formations have relatively thin hydrocarbon-rich layers, e.g. less than about 300 feet thick. Therefore, vertical mining and drilling tend to not be cost effective. In such cases, horizontal mining can be useful to recover the hydrocarbonaceous materials for formation of the permeable body. Although horizontal mining continues to be a challenging endeavor, a number of technologies have been developed and continue to be developed which can be useful in connection with the impoundments. In such cases, at least a portion of the impoundment can be formed across a horizontal layer, while other portions of the impoundment can be formed along and/or adjacent non-hydrocarbon bearing formation layers. Other mining approaches such as, but not limited to, room and pillar mining can provide an effective source of hydrocarbonaceous material with minimal waste and/or reclamation which can be transported to an impoundment and treated in accordance with these principles.\|[0054] As mentioned herein, these systems and processes allow for a large degree of control regarding properties and characteristics of the permeable body which can be designed and optimized for a given installation. Impoundments, individually and across a plurality of impoundments can be readily tailored and classified based on varying composition of materials, intended products and the like. For example, several impoundments can be dedicated to production of heavy crude oil, while others can be configured for production of lighter products and/or syn gas. Non-limiting example of potential classifications and factors can include catalyst activity, enzymatic reaction for specific products, aromatic compounds, hydrogen content, microorganism strain or purpose, upgrading process, target final product, pressure (effects product quality and type), temperature, swelling behavior, aquathermal reactions, hydrogen donor agents, heat superdisposition, garbage impoundment, sewage impoundment, reusable pipes, and others. Typically, a plurality of these factors can be used to configure impoundments in a given project area for distinct products and purposes.\|[0055] The comminuted hydrocarbonaceous material can be filled into the control infrastructure to form the permeable body in any suitable manner. Typically the comminuted hydrocarbonaceous material can be conveyed into the control infrastructure by dumping, conveyors or other suitable approaches. As mentioned previously, the permeable body can have a suitably high void volume. Indiscriminate dumping can result in excessive compaction and reduction of void volumes. Thus, the permeable body can be formed by low compaction conveying of the hydrocarbonaceous material into the infrastructure. For example, retracting conveyors can be used to deliver the material near a top surface of the permeable body as it is formed. In this way, the hydrocarbonaceous material can retain a significant void volume between particles without substantial further crushing or compaction despite some small degree of compaction which often results from lithostatic pressure as the permeable body is formed.\|[0056] Once a desired permeable body has been formed within the control infrastructure, heat can be introduced sufficient to begin removal of hydrocarbons, e.g. via pyrolysis. A suitable heat source can be thermally associated with the permeable body. Optimal operating temperatures within the permeable body can vary depending on the composition and desired products. However, as a general guideline, operating temperatures can range from about 200° F. to about 750° F. Temperature variations throughout the encapsulated volume can vary and may reach as high as 900° F. or more in some areas. In one embodiment, the operating temperature can be a relatively lower temperature to facilitate production of liquid product such as from about 200° F. to about 650° F. This heating step can be a roasting operation which results in beneficiation of the crushed ore of the permeable body. Further, one embodiment comprises controlling the temperature, pressure and other variables sufficient to produce predominantly, and in some cases substantially only, liquid product. Generally, products can include both liquid and gaseous products, while liquid products can require fewer processing steps such as scrubbers etc. The relatively high permeability of the permeable body allows for production of liquid hydrocarbon products and minimization of gaseous products, depending to some extent on the particular starting materials and operating conditions. In one embodiment, the recovery of hydrocarbon products can occur substantially in the absence of cracking within the permeable body.\|[0057] In one aspect, heat can be transferred to the permeable body via convection. Heated gases can be injected into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body. Heated gases can be produced by combustion of natural gas, hydrocarbon product, or any other suitable source. The heated gases can be imported from external sources or recovered from the process.\|[0058] Alternatively, or in combination with convective heating, a highly configurable approach can include embedding a plurality of conduits within the permeable body. The conduits can be configured for use as heating pipes, cooling pipes, heat transfer pipes, drainage pipes, or gas pipes. Further, the conduits can be dedicated to a single function or may serve multiple functions during operation of the infrastructure, i.e. heat transfer and drainage. The conduits can be formed of any suitable material, depending on the intended function. Non-limiting examples of suitable materials can include clay pipes, refractory cement pipes, refractory ECC pipes, poured in place pipes, metal pipes such as cast iron, stainless steel etc., polymer such as PVC, and the like. In one specific embodiment, all or at least a portion of the embedded conduits can comprise a degradable material. For example, non-galvanized 6″ cast iron pipes can be effectively used for single use embodiments and perform well over the useful life of the impoundment, typically less than about 2 years. Further, different portions of the plurality of conduits can be formed of different materials. Poured in place pipes can be especially useful for very large encapsulation volumes where pipe diameters exceed several feet. Such pipes can be formed using flexible wraps which retain a viscous fluid in an annular shape. For example, PVC pipes can be used as a portion of a form along with flexible wraps, where concrete or other viscous fluid is pumped into an annular space between the PVC and flexible wrap. Depending on the intended function, perforations or other apertures can be made in the conduits to allow fluids to flow between the conduits and the permeable body. Typical operating temperatures exceed the melting point of conventional polymer and resin pipes. In some embodiments, the conduits can be placed and oriented such that the conduits intentionally melt or otherwise degrade during operation of the infrastructure.\|[0059] The plurality of conduits can be readily oriented in any configuration, whether substantially horizontal, vertical, slanted, branched, or the like. At least a portion of the conduits can be oriented along predetermined pathways prior to embedding the conduits within the permeable body. The predetermined pathways can be designed to improve heat transfer, gas-liquid-solid contacting, maximize fluid delivery or removal from specific regions within the encapsulated volume, or the like. Further, at least a portion the conduits can be dedicated to heating of the permeable body. These heating conduits can be selectively perforated to allow heated gases or other fluids to convectively heat and mix throughout the permeable body. The perforations can be located and sized to optimize even and/or controlled heating throughout the permeable body. Alternatively, the heating conduits can form a closed loop such that heating gases or fluids are segregated from the permeable body. Thus, a “closed loop” does not necessarily require recirculation, rather isolation of heating fluid from the permeable body. In this manner, heating can be accomplished primarily or substantially only through thermal conduction across the conduit walls from the heating fluids into the permeable body. Heating in a closed loop allows for prevention of mass transfer between the heating fluid and permeable body and can reduce formation and/or extraction of gaseous hydrocarbon products.\|[0060] During the heating or roasting of the permeable body, localized areas of heat which exceed parent rock decomposition temperatures, often above about 900° F., can reduce yields and form carbon dioxide and undesirable contaminating compounds which can lead to leachates containing heavy metals, soluble organics and the like. The heating conduits can allow for substantial elimination of such localized hot spots while maintaining a vast majority of the permeable body within a desired temperature range. The degree of uniformity in temperature can be a balance of cost (e.g. for additional heating conduits) versus yields. However, at least about 85% of the permeable body can readily be maintained within about 5-10% of a target temperature range with substantially no hot spots, i.e. exceeding the decomposition temperature of the hydrocarbonaceous materials such as about 800° F. and in many cases about 900° F. Thus, operated as described herein, the systems can allow for recovery of hydrocarbons while eliminating or substantially avoiding production of undesirable leachates. Although products can vary considerably depending on the starting materials, high quality liquid and gaseous products are possible. In accordance with one embodiment, a crushed oil shale material can produce a liquid product having an API from about 30 to about 45, with about 33 to about 38 being currently typical, directly from the oil shale without additional treatment. Interestingly, practice of these principles has led to an understanding that pressure appears to be a much less influential factor on the quality of recovered hydrocarbons than temperature and heating times. Although heating times can vary considerably, depending on void space, permeable body composition, quality, etc., as a general guideline times can range from a few days (i.e. 3-4 days) up to about one year. In one specific example, heating times can range from about 2 weeks to about 4 months. Under-heating oil shale at short residence times, i.e. minutes to several hours, can lead to formation of leachable and/or somewhat volatile hydrocarbons. Accordingly, these systems and processes allow for extended residence times at moderate temperatures such that organics present in oil shale can be volatilized and/or carbonized, leaving insubstantial leachable organics. In addition, the underlying shale is not generally decomposed or altered which reduces soluble salt formation.\|[0061] Further, conduits can be oriented among a plurality of impoundments and/or control infrastructures to transfer fluids and/or heat between the structures. The conduits can be welded to one another using conventional welding or the like. Further, the conduits can include junctions which allow for rotation and or small amounts of movement during expansion and subsidence of material in the permeable body. Additionally, the conduits can include a support system which acts to support the assembly of conduits prior to and during filling of the encapsulated volume, as well as during operation. For example, during heating flows of fluids, heating and the like can cause expansion (fracturing or popcorn effect) or subsidence sufficient to create potentially damaging stress and strain on the conduits and associated junctions. A truss support system or other similar anchoring members can be useful in reducing damage to the conduits. The anchoring members can include cement blocks, 1-beams, rebar, columns, etc. which can be associated with walls of the impoundment, including side walls, floors and ceilings.\|[0062] Alternatively, the conduits can be completely constructed and assembled prior to introduction of any mined materials into the encapsulated volume. Care and planning can be considered in designing the predetermined pathways of the conduits and method of filling the volume in order to prevent damage to the conduits during the filling process as the conduits are buried. Thus, as a general rule, the conduits used are oriented ab initio, or prior to embedding in the permeable body such that they are non-drilled. As a result, construction of the conduits and placement thereof can be performed without extensive core drilling and/or complicated machinery associated with well-bore or horizontal drilling. Rather, horizontal or any other orientation of conduit can be readily achieved by assembling the desired predetermined pathways prior to, or contemporaneous with, filling the infrastructure with the mined hydrocarbonaceous material. The non-drilled, hand/crane-placed conduits oriented in various geometric patterns can be laid with valve controlled connecting points which yield precise and closely monitored heating within the capsule impoundment. The ability to place and layer conduits including connecting, bypass and flow valves, and direct injection and exit points, allow for precision temperature and heating rates, precision pressure and pressurization rates, and precision fluid and gas ingress, egress and composition admixtures. For example, when a bacteria, enzyme, or other biological material is used, optimal temperatures can be readily maintained throughout the permeable body to increase performance, reaction, and reliability of such biomaterials.\|[0063] The conduits will generally pass through walls of the constructed infrastructure at various points. Due to temperature differences and tolerances, it can be beneficial to include an insulating material at the interface between the wall and the conduits. The dimensions of this interface can be minimized while also allowing space for thermal expansion differences during startup, steady-state operation, fluctuating operating conditions, and shutdown of the infrastructure. The interface can also involve insulating materials and sealant devices which prevent uncontrolled egress of hydrocarbons or other materials from the control infrastructure. Non-limiting examples of suitable materials can include high temperature gaskets, metal alloys, ceramics, clay or mineral liners, composites or other materials which having melting points above typical operating temperatures and act as a continuation of the permeability control provided by walls of the control infrastructure.\|[0064] Further, walls of the constructed infrastructure can be configured to minimize heat loss. In one aspect, the walls can be constructed having a substantially uniform thickness which is optimized to provide sufficient mechanical strength while also minimizing the volume of wall material through which the conduits pass. Specifically, excessively thick walls can reduce the amount of heat which is transferred into the permeable body by absorbing the same through conduction. Conversely, the walls can also act as a thermal barrier to somewhat insulate the permeable body and retain heat therein during operation.\|[0065] In one embodiment, fluid and gas compounds within the permeable body can be altered for desired extractive products using, as an example, induced pressure through gases or piled lithostatic pressure from piled rubble. Thus, some degree of upgrading and/or modification can be accomplished simultaneous with the recovery process. Further, certain hydrocarbonaceous materials can require treatment using specific diluents or other materials. For example, treatment of tar sands can be readily accomplished by steam injection or solvent injection to facilitate separation of bitumen from sand particles according to well known mechanisms.\|[0066] With the above description in mind, FIG. 1 depicts a side view of one embodiment showing an engineered capsule containment and extraction impoundment 100 where existing grade 108 is used primarily as support for the impermeable floor layer 112. Exterior capsule impoundment side walls 102 provide containment and can, but need not be, subdivided by interior walls 104. Subdividing can create separate containment capsules 122 within a greater capsule containment of the impoundment 100 which can be any geometry, size or subdivision. Further subdivisions can be horizontally or vertically stacked. By creating separate containment capsules 122 or chambers, classification of lower grade materials, varied gases, varied liquids, varied process stages, varied enzymes or microbiology types, or other desired and staged processes can be readily accommodated. Sectioned capsules constructed as silos within larger constructed capsules can also be designed to provide staged and sequenced processing, temperatures, gas and fluid compositions and thermal transfers. Such sectioned capsules can provide additional environmental monitoring and can be built of lined and engineered tailings berms similar to the primary exterior walls. In one embodiment, sections within the impoundment 100 can be used to place materials in isolation, in the absence of external heat, or with the intent of limited or controlled combustion or solvent application. Lower content hydrocarbon bearing material can be useful as a combustion material or as fill or a berm wall building material. Material which does not meet a various cut-off grade thresholds can also be sequestered without alteration in an impoundment dedicated for such purpose. In such embodiments, such areas may be completely isolated or bypassed by heat, solvents, gases, liquids, or the like. Optional monitoring devices and/or equipment can be permanently or temporarily installed within the impoundment or outside perimeters of the impoundments in order to verify containment of the sequestered material.\|[0067] Walls 102 and 104 as well as cap 116 and impermeable layer 112 can be engineered and reinforced by gabions 146 and or geogrid 148 layered in fill compaction. Alternatively, these walls 102, 104, 116 and 112 which comprise the permeability control impoundment and collectively define the encapsulated volume can be formed of any other suitable material as previously described. In this embodiment, the impoundment 100 includes side walls 102 and 104 which are self-supporting. In one embodiment, tailings berms, walls, and floors can be compacted and engineered for structure as well as permeability. The use of compacted geogrids and other deadman structures for support of berms and embankments can be included prior to or incorporated with permeability control layers which may include sand, clay, bentonite clay, gravel, cement, grout, reinforced cement, refractory cements, insulations, geo-membranes, drainpipes, temperature resistant insulations of penetrating heated pipes, etc.\|[0068] In one alternative embodiment, the permeability control impoundment can include side walls which are compacted earth and/or undisturbed geological formations while the cap and floors are impermeable. Specifically, in such embodiments an impermeable cap can be used to prevent uncontrolled escape of volatiles and gases from the impoundment such that appropriate gas collection outlets can be used. Similarly, an impermeable floor can be used to contain and direct collected liquids to a suitable outlet such the drain system 133 to remove liquid products from lower regions of the impoundment. Although impermeable side walls can be desirable in some embodiments, such are not always required. In some cases, side walls can be exposed undisturbed earth or compacted fill or earth, or other permeable material. Having permeable side walls may allow some small egress of gases and/or liquids from the impoundment.\|[0069] However, it may be desirable to have the impoundment constructed such that a positive pressure is maintained therein thereby preventing the introduction of air or other oxidizing gases from entering into the impoundment. The presence of oxygen can result in polymerization and gumming of the hydrocarbons and other contents within the impoundment. Further, the presence of oxygen can induce combustion within the system.\|[0070] Although not shown, above, below, around and adjacent to constructed capsule containment vessels environmental hydrology measures can be engineered to redirect surface water away from the capsule walls, floors, caps, etc. during operation. Further, gravity assisted drainage pipes and mechanisms can be utilized to aggregate and channel fluids, liquids or solvents within the encapsulated volume to central gathering, pumping, condensing, heating, staging and discharge pipes, silos, tanks, and/or wells as needed. In a similar manner, steam and/or water which is intentionally introduce, e.g. for tar sands bitumen treatment, can be recycled.\|[0071] Once wall structures 102 and 104 have been constructed above a constructed and impermeable floor layer 112 which commences from ground surface 106, the mined rubble 120 (which may be crushed or classified according to size or hydrocarbon richness), can be placed in layers upon (or next to) placed tubular heating pipes 118, fluid drainage pipes 124, and, or gas gathering or injection pipes 126. These pipes can be oriented and designed in any optimal flow pattern, angle, length, size, volume, intersection, grid, wall sizing, alloy construction, perforation design, injection rate, and extraction rate. In some cases, pipes such as those used for heat transfer can be connected to, recycled through or derive heat from heat source 134. Alternatively, or in combination with, recovered gases can be condensed by a condenser 140. Heat recovered by the condenser can be optionally used to supplement heating of the permeable body or for other process needs.\|[0072] Heat source 134 can derive, amplify, gather, create, combine, separate, transmit or include heat derived from any suitable heat source including, but not limited to, fuel cells (e.g. solid oxide fuel cells, molten carbonate fuel cells and the like), solar sources, wind sources, hydrocarbon liquid or gas combustion heaters, geothermal heat sources, nuclear power plant, coal fired power plant, radio frequency generated heat, wave energy, flameless combustors, natural distributed combustors, or any combination thereof. In some cases, electrical resistive heaters or other heaters can be used, although fuel cells and combustion-based heaters are particularly effective. In some locations, geothermal water can be circulated to the surface in adequate amounts to heat the permeable body and directed into the infrastructure.\|[0073] In another embodiment, electrically conductive material can be distributed throughout the permeable body and an electric current can be passed through the conductive material sufficient to generate heat. The electrically conductive material can include, but is not limited to, metal pieces or beads, conductive cement, metal coated particles, metal-ceramic composites, conductive semi-metal carbides, calcined petroleum coke, laid wire, combinations of these materials, and the like. The electrically conductive material can be premixed having various mesh sizes or the materials can be introduced into the permeable body subsequent to formation of the permeable body.\|[0074] Liquids or gases can transfer heat from heat source 134, or in another embodiment, in the cases of hydrocarbon liquid or gas combustion, radio frequency generators (microwaves), or fuel cells all can, but need not, actually generate heat inside of capsule impoundment area 114 or 122. In one embodiment, heating of the permeable body can be accomplished by convective heating from hydrocarbon combustion. Of particular interest is hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen. Stoichiometric conditions can allow for significantly increased heat gas temperatures. Stoichiometric combustion can employ but does not generally require a pure oxygen source which can be provided by known technologies including, but not limited to, oxygen concentrators, membranes, electrolysis, and the like. In some embodiments oxygen can be provided from air with stoichiometric amounts of oxygen and hydrogen. Combustion off gas can be directed to an ultra-high temperature heat exchanger, e.g. a ceramic or other suitable material having an operating temperature above about 2500° F. Air obtained from ambient or recycled from other processes can be heated via the ultra high temperature heat exchanger and then sent to the impoundment for heating of the permeable body. The combustion off gases can then be sequestered without the need for further separation, i.e. because the off gas is predominantly carbon dioxide and water.\|[0075] In order to minimize heat losses, distances can be minimized between the combustion chamber, heat exchanger and impoundments. Therefore, in one specific detailed embodiment portable combustors can be attached to individual heating conduits or smaller sections of conduits. Portable combustors or burners can individually provide from about 100,000 Btu to about 1,000,000 Btu with about 600,000 Btu per pipe generally being sufficient.\|[0076] Alternatively, in-capsule combustion can be initiated inside of isolated capsules within a primary constructed capsule containment structure. This process partially combusts hydrocarbonaceous material to provide heat and intrinsic pyrolysis. Unwanted air emissions 144 can be captured and sequestered in a formation 108 once derived from capsule containment 114, 122 or from heat source 134 and delivered by a drilled well bore 142. Heat source 134 can also create electricity and transmit, transform or power via electrical transmission lines 150. The liquids or gases extracted from capsule impoundment treatment area 114 or 122 can be stored in a nearby holding tank 136 or within a capsule containment 114 or 122. For example, the impermeable floor layer 112 can include a sloped area 110 which directs liquids towards drain system 133 where liquids are directed to the holding tank.\|[0077] As rubble material 120 is placed with piping 118, 124, 126, and 128, various measurement devices or sensors 130 are envisioned to monitor temperature, pressure, fluids, gases, compositions, heating rates, density, and all other process attributes during the extractive process within, around, or underneath the engineered capsule containment impoundment 100. Such monitoring devices and sensors 130 can be distributed anywhere within, around, part of, connected to, or on top of placed piping 118, 124, 126, and 128 or, on top of, covered by, or buried within rubble material 120 or impermeable barrier zone 112.\|[0078] As placed rubble material 120 fills the capsule treatment area 114 or 122, 120 becomes the ceiling support for engineered impermeable cap barrier zone 138, and wall barrier construction 170, which may include any combination of impermeability and engineered fluid and gas barrier or constructed capsule construction comprising those which may make up 112 including, but not limited to clay 162, compacted fill or import material 164, cement or refractory cement containing material 166, geo synthetic membrane, liner or insulation 168. Above 138, fill material can be oriented as ceiling cap 116 is placed to create lithostatic pressure upon the capsule treatment areas 114 or 122. Covering the permeable body with compacted fill sufficient to create an increased lithostatic pressure within the permeable body can be useful in further increasing hydrocarbon product quality. A compacted fill ceiling can substantially cover the permeable body, while the permeable body in return can substantially support the compacted fill ceiling. The compacted fill ceiling can further be sufficiently impermeable to removed hydrocarbon or an additional layer of permeability control material can be added in a similar manner as side and/or floor walls. Additional pressure can be introduced into extraction capsule treatment area 114 or 122 by increasing any gas or fluid once extracted, treated or recycled, as the case may be, via any of piping 118, 124, 126, or 128. In one embodiment the additional pressure is sufficient to maintain a positive pressure within the treatment area and is provided by the introduction of a non-oxidizing gas such as hydrogen, nitrogen, propane, carbon dioxide or any other gas which provides an inert atmosphere within the treatment area. Other potential flushing gases can include but are not limited to hydrocarbon gases. All relative measurements, optimization rates, injection rates, extraction rates, temperatures, heating rates, flow rates, pressure rates, capacity indicators, chemical compositions, or other data relative to the process of heating, extraction, stabilization, sequestration, impoundment, upgrading, refining or structure analysis within the capsule impoundment 100 are envisioned through connection to a computing device 132 which operates computer software for the management, calculation and optimization of the entire process. Further, core drilling, geological reserve analysis and assay modeling of a formation prior to blasting, mining and hauling (or at any time before, after or during such tasks) can serve as data input feeds into computer controlled mechanisms that operate software to identify optimal placements, dimensions, volumes and designs calibrated and cross referenced to desired production rate, pressure, temperature, heat input rates, gas weight percentages, gas injection compositions, heat capacity, permeability, porosity, chemical and mineral composition, compaction, density. Such analysis and determinations may include other factors like weather data factors such as temperature and air moisture content impacting the overall performance of the constructed infrastructure. Other data such as ore moisture content, hydrocarbon richness, weight, mesh size, and mineral and geological composition can be utilized as inputs including time value of money data sets yielding project cash flows, debt service and internal rates of return.\|[0079] FIG. 2A shows a collection of impoundments including an uncovered or uncapped capsule impoundment 100, containing sectioned capsule impoundments 122 inside of a mining quarry 200 with various elevations of bench mining. FIG. 2B illustrates a single impoundment 122 without associated conduits and other aspects merely for clarity. This impoundment can be similar to that illustrated in FIG. 1 or any other configuration. In some embodiments, it is envisioned that mining rubble can be transferred down chutes 230 or via conveyors 232 to the quarry capsule impoundments 100 and 122 without any need of mining haul trucks.\|[0080] FIG. 3 shows the engineered permeability barriers 112 below capsule impoundment 100 resting on exiting grade 106 of formation 108 with cap covering material or fill 302 on the sides and top of capsule impoundment 100 to ultimately (following the process) cover and reclaim a new earth surface 300. Indigenous plants which may have been temporarily moved from the area may be replanted such as trees 306. The constructed infrastructures can generally be single use structures which can be readily and securely shut down with minimal additional remediation. This can dramatically reduce costs associated with moving large volumes of spent materials. However, in some circumstances the constructed infrastructures can be excavated and reused. Some equipment such as radio frequency (RF) mechanisms, tubulars, devices and emitters may be recovered from within the constructed impoundment upon completion of hydrocarbon recovery.\|[0081] FIG. 4 shows computer means 130 controlling various property inputs and outputs of conduits 118, 126, or 128 connected to heat source 134 during the process among the subdivided impoundments 122 within a collective impoundment 100 to control heating of the permeable body. Similarly, liquid and vapor collected from the impoundments can be monitored and collected in tank 136 and condenser 140, respectively. Condensed liquids from the condenser can be collected in tank 141, while non-condensable vapor collected at unit 143. As described previously, the liquid and vapor products can be combined or more often left as separate products depending on condensability, target product, and the like. A portion of the vapor product can be optionally condensed and combined with the liquid products in tank 136. However, much of the vapor product will be C4 and lighter gases which can be burned, sold or used within the process. For example, hydrogen gas may be recovered using conventional gas separation and used to hydrotreat the liquid products according to conventional upgrading methods, e.g. catalytic, etc. or the non-condensable gaseous product can be burned to produce heat for use in heating the permeable body, heating an adjacent or nearby impoundment, heating service or personnel areas, or satisfying other process heat requirements. The constructed infrastructure can include thermocouples, pressure meters, flow meters, fluid dispersion sensors, richness sensors and any other conventional process control devices distributed throughout the constructed infrastructure. These devices can be each operatively associated with a computer such that heating rates, product flow rates, and pressures can be monitored or altered during heating of the permeable body. Optionally, in-place agitation can be performed using, for example, ultrasonic generators which are associated with the permeable body. Such agitation can facilitate separation and pyrolysis of hydrocarbons from the underlying solid materials with which they are associated. Further, sufficient agitation can reduce clogging and agglomeration throughout the permeable body and the conduits.\|[0082] FIG. 5 shows how any of the conduits can be used to transfer heat in any form of gas, liquid or heat via transfer means 510 from any sectioned capsule impoundment to another. Then, cooled fluid can be conveyed via heat transfer means 512 to the heat originating capsule 500, or heat originating source 134 to pick up more heat from capsule 500 to be again recirculated to a destination capsule 522. Thus, various conduits can be used to transfer heat from one impoundment to another in order to recycle heat and manage energy usage to minimize energy losses.\|[0083] In yet another aspect, a hydrogen donor agent can be introduced into the permeable body during the step of heating. The hydrogen donor agent can be any composition which is capable of hydrogenation of the hydrocarbons and can optionally be a reducing agent. Non-limiting examples of suitable hydrogen donor agents can include synthesis gas, propane, methane, hydrogen, natural gas, natural gas condensate, industrial solvents such as acetones, toluenes, benzenes, xylenes, cumenes, cyclopentanes, cyclohexanes, lower alkenes (C4-C10), terpenes, substituted compounds of these solvents, etc., and the like. Further, the recovered hydrocarbons can be subjected to hydrotreating either within the permeable body or subsequent to collection. Advantageously, hydrogen recovered from the gas products can be reintroduced into the liquid product for upgrading. Regardless, hydrotreating or hydrodesulfurization can be very useful in reducing nitrogen and sulfur content in final hydrocarbon products. Optionally, catalysts can be introduced to facilitate such reactions. In addition, introduction of light hydrocarbons into the permeable body can result in reforming reactions which reduce the molecular weight, while increasing the hydrogen to carbon ratio. This is particularly advantageous due at least in part to high permeability of the permeable body, e.g. often around 30%-40% void volume although void volume can generally vary from about 10% to about 50% void volume. Light hydrocarbons which can be injected can be any which provide reforming to recovered hydrocarbons. Non-limiting examples of suitable light hydrocarbons include natural gas, natural gas condensates, industrial solvents, hydrogen donor agents, and other hydrocarbons having ten or fewer carbons, and often five or fewer carbons. Currently, natural gas is an effective, convenient and plentiful light hydrocarbon. As mentioned previously, various solvents or other additives can also be added to aid in extraction of hydrocarbon products from the oil shale and can often also increase fluidity.\|[0084] The light hydrocarbon can be introduced into the permeable body by conveying the same through a delivery conduit having an open end in fluid communication with a lower portion of the permeable body such that the light hydrocarbons (which are a gas under normal operating conditions) permeate up through the permeable body. Alternatively, this same approach can be applied to recovered hydrocarbons which are first delivered to an empty impoundment. In this way, the impoundment can act as a holding tank for direct products from a nearby impoundment and as a reformer or upgrader. In this embodiment, the impoundment can be at least partially filled with a liquid product where the gaseous light hydrocarbon is passed through and allowed to contact the liquid hydrocarbon products at temperatures and conditions sufficient to achieve reforming in accordance with well known processes. Optional reforming catalysts which include metals such as Pd, Ni or other suitable catalytically active metals can also be included in the liquid product within the impoundment. The addition of catalysts can serve to lower and/or adjust reforming temperature and/or pressure for particular liquid products. Further, the impoundments can be readily formed at almost any depth. Thus, optimal reforming pressures (or recovery pressures when using impoundment depth as pressure control measure for recovery from a permeable body) can be designed based on hydrostatic pressure due to the amount of liquid in the impoundment and the height of the impoundment, i.e. P=ρgh. In addition, the pressure can vary considerably over the height of the impoundment sufficient to provide multiple reforming zones and tailorable pressures. Generally, pressures within the permeable body can be sufficient to achieve substantially only liquid extraction, although some minor volumes of vapor may be produced depending on the particular composition of the permeable body. As a general guideline, pressures can range from about 5 atm to about 50 atm, although pressures from about 6 atm to about 20 atm can be particularly useful. However, any pressure greater than about atmospheric can be used.\|[0085] In certain instances the maintaining of a positive pressure within the enclosed capsule, relative to the outside atmosphere, has certain advantages. For example, a positive pressure prevents unwanted gases from entering into the impoundment during the hydrocarbon removal process and further expedites the removal of hydrocarbons from within the impoundment. Maintaining a positive pressure by means of a non-oxidizing gas reduces the likelihood of unwanted combustion and retards or prevents polymerization of lighter hydrocarbons which can form deposits on pipes or other infrastructure within the impoundment. Also, a positive pressure enables the flushing of the system in the event of certain events or happenings. One example might be in the event there is an interruption of the processing of the hydrocarbonaceous material and the collection of hydrocarbons due to a leak or other unwanted escape of fluids from within the impoundment. A positive pressure allows for the almost instantaneous introduction of non-oxidizing gases at a predetermined temperature, preferably a cooling temperature, to flush hydrocarbons and other vaporous components from the permeable body and within the impoundment so as to maintain an inert environment until any problem is detected and corrected. As previously noted gases such as hydrogen, nitrogen, propane, carbon dioxide, hydrocarbons, and the like can be used to flush the impoundment. Although any functional positive pressure can be suitable, pressure can generally be from about 1.01 atm to about 10 atm, and in one aspect from about 1.1 atm to about 4 atm.\|[0086] Further, once the hydrocarbon production stage is completed, the impoundment can be flushed with a non-oxidizing gas in order to remove further recoverable hydrocarbons from the impoundment. Such flushing can be accomplished in stages or in increments of temperature reduction or any other means to recover meaningful quantities of hydrocarbons. It may be beneficial to allow such flushing and cooling in increments such as to maximize the recovery of hydrocarbons while, at the same time, prepare the hydrocarbon lean shale or other materials, for further processing and/or pacification. The flushing times will obviously depend on the size of the permeable body and the impoundment and can be accomplished in a matter of hours, days or even weeks.\|[0087] Also, the lean shale or other inorganic matter resulting from the termination of the hydrocarbon removal process may still contain other components such as heavy metals, precious metals or other mineral components in the permeable body that can be extracted in further processing steps. Certain deposits may contain radioactive materials that require further processing and/or impounding in order to comply with governmental regulations.\|[0088] In one embodiment, extracted crude has fines precipitated out within the subdivided capsules. Extracted fluids and gases can be treated for the removal of fines and dust particles. Separation of fines from shale oil can be accomplished by techniques such as, but not limited to, hot gas filtering, precipitation, and heavy oil recycling.\|[0089] Hydrocarbon products recovered from the permeable body can be further processed (e.g. refined) or used as produced. Any condensable gaseous products can be condensed by cooling and collection, while non-condensable gases can be collected, burned as fuel, reinjected, or otherwise utilized or disposed of Optionally, mobile equipment can be used to collect gases. These units can be readily oriented proximate to the control infrastructure and the gaseous product directed thereto via suitable conduits from an upper region of the control infrastructure.\|[0090] In yet another alternative embodiment, heat within the permeable body can be recovered subsequent to primary recovery of hydrocarbon materials therefrom. For example, a large amount of heat is retained in the permeable body. In one optional embodiment, the permeable body can be flooded with a heat transfer fluid such as water to form a heated fluid, e.g. heated water and/or steam. At the same time, this process can facilitate removal of some residual hydrocarbon products via a physical rinsing of the spent shale solids. In some cases, the introduction of water and presence of steam can result in water gas shift reactions and formation of synthesis gas. Steam recovered from this process can be used to drive a generator, directed to another nearby infrastructure, or otherwise used. Hydrocarbons and/or synthesis gas can be separated from the steam or heated fluid by conventional methods.\|[0091] Although the methods and infrastructure allow for improved permeability and control of operating conditions, significant quantities of unrecovered hydrocarbons, precious metals, minerals, sodium bicarbonate or other commercially valuable materials often remain in the permeable body. Therefore, a selective solvent can be injected or introduced into the permeable body. Typically, this can be done subsequent to collecting the hydrocarbons, although certain selective solvents can be beneficially used prior to heating and/or collection. This can be done using one or more of the existing conduits or by direct injection and percolation through the permeable body. The selective solvent or leachate can be chosen as a solvent for one or more target materials, e.g. minerals, precious metal, heavy metals, hydrocarbons, or sodium bicarbonate. In one specific embodiment, steam or carbon dioxide can be used as a rinse of the permeable body to dislodge at least a portion of any remaining hydrocarbons. This can be beneficial not only in removing potentially valuable secondary products, but also in cleaning remaining spent materials of trace heavy metal or inorganics to below detectable levels in order to comply with regulatory standards or to prevent inadvertent leaching of materials at a future date.\|[0092] More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body. Typically, such recovery of materials can be performed prior to heat treatment of the permeable body. Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like. For example, heavy metals, bauxite or aluminum, and mercury can be removed by flooding the permeable body with an appropriate solvent and recirculating the resulting leachate through appropriately designed ion exchange resins (e.g. beads, membranes, etc.).\|[0093] Similarly, bioextraction, bio leaching, biorecovery, or bioremediation of hydrocarbon material, spent materials, or precious metals can be performed to further improve remediation, extract valuable metals, and restoration of spent material to environmentally acceptable standards. In such bioextraction scenarios, conduits can be used to inject catalyzing gases as a precursor which helps to encourage bioreaction and growth. Such microorganisms and enzymes can biochemically oxidize the ore body or material or cellulosic or other biomass material prior to an ore solvent extraction via bio-oxidation. For example, a perforated pipe or other mechanism can be used to inject a light hydrocarbon (e.g. methane, ethane, propane or butane) into the permeable body sufficient to stimulate growth and action of native bacteria. Bacteria can be native or introduced and may grow under aerobic or anaerobic conditions. Such bacteria can release metals from the permeable body which can then be recovered via flushing with a suitable solvent or other suitable recovery methods. The recovered metals can then be precipitated out using conventional methods.\|[0094] Synthesis gas can also be recovered from the permeable body during the step of heating. Various stages of gas production can be manipulated through processes which raise or lower operating temperatures within the encapsulated volume and adjust other inputs into the impoundment to produce synthetic gases which can include but are not limited to, carbon monoxide, hydrogen, hydrogen sulfide, hydrocarbons, ammonia, water, nitrogen or various combinations thereof. In one embodiment, temperature and pressure can be controlled within the permeable body to lower CO2 emissions as synthetic gases are extracted.\|[0095] Hydrocarbon product recovered from the constructed infrastructures can most often be further processed, e.g. by upgrading, refining, etc. Sulfur from related upgrading and refining processing can be isolated in various constructed sulfur capsules within the greater structured impoundment capsule. Constructed sulfur capsules can be spent constructed infrastructures or dedicated for the purpose of storage and isolation after desulfurization.\|[0096] Similarly, spent hydrocarbonaceous material remaining in the constructed infrastructure can be utilized in the production of cement and aggregate products for use in construction or stabilization of the infrastructure itself or in the formation of offsite constructed infrastructures. Such cement products made with the spent shale may include, but are not limited to, mixtures with Portland cement, calcium salt, volcanic ash, perlite, synthetic nano carbons, sand, fiber glass, crushed glass, asphalt, tar, binding resins, cellulosic plant fibers, and the like.\|[0097] In still another embodiment, injection, monitoring and production conduits or extraction egresses can be incorporated into any pattern or placement within the constructed infrastructure. Monitoring wells and constructed geo membrane layers beneath or outside of the constructed capsule containment can be employed to monitor unwanted fluid and moisture migration outside of containment boundaries and the constructed infrastructure.\|[0098] Although a filled and prepared constructed infrastructure can often be immediately heated to recover hydrocarbons, this is not required. For example, a constructed infrastructure which is built and filled with mined hydro carbonaceous material can be left in place as a proven reserve. Such structures are less susceptible to explosion or damage due to terrorist activity and can also provide strategic reserves of unprocessed petroleum products, with classified and known properties so that economic valuations can be increased and more predictable. Long term petroleum storage often faces quality deterioration issues over time. Thus, these approaches can optionally be used for long term quality insurance and storage with reduced concerns regarding breakdown and degradation of hydrocarbon products.\|[0099] In still another aspect, the high quality liquid product can be blended with more viscous lower quality (e.g. lower API) hydrocarbon products. For example, kerogen oil produced from the impoundments can be blended with bitumen to form a blended oil. The bitumen is typically not transportable through an extended pipeline under conventional and accepted pipeline standards and can have a viscosity substantially above and an API substantially below that of the kerogen oil. By blending the kerogen oil and bitumen, the blended oil can be rendered transportable without the use of additional diluents or other viscosity or API modifiers. As a result, the blended oil can be pumped through a pipeline without requiring additional treatments to remove a diluent or returning such diluents via a secondary pipeline. Conventionally, bitumen is combined with a diluent such as natural gas condensate or other low molecular weight liquids, to allow pumping to a remote location. The diluent is removed and returned via a second pipeline back to the bitumen source. These approaches allow for elimination of returning diluent and simultaneous upgrading of the bitumen.\|[0100] Although these processes are mining-dependent, they are not limited or encumbered to conventional aboveground (ex-situ) retorting processes. This approach improves upon the benefits of surface retorts including better process control of temperature, pressure, injection rates, fluid and gas compositions, product quality and better permeability due to processing and heating mined rubble. These advantages are available while still addressing the volume, handling, and scalability issues most fabricated surface retorts cannot provide.\|[0101] Other improvements which can be realized are related to environmental protection. Conventional surface retorts have had the problem of spent shale after it has been mined and has passed through a surface retort. Spent shale which has been thermally altered requires special handling to reclaim and isolate from surface drainage basins and underground aquifers. This approach addresses reclamation and retorting in a uniquely combined approach. In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants. This approach uniquely provides solutions to problems for not just one, but many problems, and in an integrated approach. As a result, significant benefits to the public can be achieved in terms of energy production, economic opportunity, environmental stewardship and energy output.\|[0102] It is to be understood that the above-referenced arrangements are illustrative of the application for the principles of the present invention. Thus, while the present invention has been described above in connection with the exemplary embodiments, it will be apparent to those of ordinary skill in the art that numerous modifications and alternative arrangements can be made without departing from the principles and concepts of the invention as set forth in the claims.	Family Number\|(35292)\|35292\|Title\|(EA201171025 A1)\|Methods for recovering hydrocarbons from carbon dioxide capture material using constructed infrastructure and associated overpressure systems\|Advantages / Prev. Drawbacks\|(CN102395653B B)\|Other methods include in situ radio frequency methods ( microwaves ) and " modified " in situ processes where underground mining , blasting and retorting have been used in combination to produce crushed rock from a formation to allow for better heat transfer and product removal . \|(CN102395653 A)\|Other methods include in situ radio frequency methods ( microwaves ) and " modified " in situ processes where underground mining , blasting and retorting have been used in combination to produce crushed rock from a formation to allow for better heat transfer and product removal . \|	Basic materials chemistry\|Civil engineering\|Materials, metallurgy	C10B-047/02\|C10B-053/06\|C10G-001/02\|C10G-001/04		C10B-047/02\|C10B-053/06\|C10G-001/02\|C10G-001/04	C01G-009/00\|C10B-047/02\|C10B-053/06\|C10G\|C10G-001/02\|C10G-001/04\|C10G-009/00\|E21B\|E21B-043/00	C01G-009/00\|C10B-047/02\|C10B-053/06\|C10G\|C10G-001/00\|C10G-001/02\|C10G-001/04\|C10G-009/00\|C10G-031/00\|C10G-031/06\|E21B\|E21B-043/00	PCLO=208400000\|PCLX=299006000\|PCLX=299003000\|PCLX=052169800\|PCLX=405129270\|PCLX=405129570\|PCLX=405130000\|PCLX=405128350\|PCLX=405128650\|PCLX=405128550\|PCLX=405128850\|PCLX=405129850\|PCLX=405128400\|PCLX=299002000\|PCLX=299014000\|PCLX=405128600\|PCLX=405129700\|PCLX=405128900\|PCLX=405128800	PCLO=208400000 PCLX=299002000 PCLX=299003000 PCLX=299006000 PCLX=299014000 PCLX=405128350 PCLX=405128400 PCLX=405128550 PCLX=405128600 PCLX=405128650 PCLX=405128800 PCLX=405128850 PCLX=405128900 PCLX=405129270 PCLX=405129570 PCLX=405129700 PCLX=405129850 PCLX=405130000 PCLX=052169800\|PCLO=208390000 PCLX=208177000 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WHO=Examiner SELF=Y\|US20080190815 1861751 WHO=Third_party SELF=Y\|US20080190816 1861751 WHO=Examiner SELF=Y\|US20080190816 1861751 WHO=Third_party SELF=Y\|US20080190818 1861751 WHO=Examiner SELF=Y\|US20080190818 1861751 WHO=Third_party SELF=Y\|US7862705 1861751 WHO=Third_party SELF=Y\|US7862706 43740497 WHO=Examiner SELF=Y\|US7862706 43740497 WHO=Third_party SELF=Y\|WO200898177 1861751 WHO=Third_party SELF=Y\|WO200898177 1861751 WHO=Examiner SELF=Y\|WO200898177 1861751 WHO=Examiner SELF=Y\|US20090190815 14923308 WHO=Examiner SELF=N\|US20060213657 1632664 WHO=Examiner SELF=N\|US20060213657 1632664 WHO=Third_party SELF=N\|JP2005306721 32305683 WHO=Third_party SELF=N\|US20070023186 1767434 WHO=Examiner SELF=N\|US20070023186 1767434 WHO=Third_party SELF=N\|US7121342 1761158 WHO=Third_party SELF=N\|US20070000662 61974990 WHO=Examiner SELF=N\|US20070000662 61974990 WHO=Third_party SELF=N\|US7091460 1781771 WHO=Examiner SELF=N\|US7091460 1781771 WHO=Third_party SELF=N\|US7073578 60130161 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43481366 WHO=Applicant SELF=N\|US7090013 88621749 WHO=Examiner SELF=N\|US7090013 88621749 WHO=Applicant SELF=N\|US7114566 88621749 WHO=Third_party SELF=N\|US6929330 1438851 WHO=Examiner SELF=N\|US6929330 1438851 WHO=Applicant SELF=N\|US6875356 43410084 WHO=Examiner SELF=N\|US6875356 43410084 WHO=Applicant SELF=N\|US6854328 43406177 WHO=Examiner SELF=N\|US6918443 1632664 WHO=Examiner SELF=N\|US6918443 1632664 WHO=Applicant SELF=N\|US6923257 1632664 WHO=Examiner SELF=N\|US6923257 1632664 WHO=Applicant SELF=N\|US6951247 1632664 WHO=Applicant SELF=N\|US6991033 1632664 WHO=Examiner SELF=N\|US6991033 1632664 WHO=Applicant SELF=N\|US7004247 1632664 WHO=Examiner SELF=N\|US7004247 1632664 WHO=Applicant SELF=N\|US7004251 1632664 WHO=Examiner SELF=N\|US7004251 1632664 WHO=Applicant SELF=N\|US7032660 1632664 WHO=Examiner SELF=N\|US7032660 1632664 WHO=Applicant SELF=N\|US7040397 1632664 WHO=Examiner SELF=N\|US7040397 1632664 WHO=Applicant SELF=N\|US7040399 1632664 WHO=Examiner SELF=N\|US7040399 1632664 WHO=Applicant SELF=N\|US7051811 1632664 WHO=Examiner SELF=N\|US7051811 1632664 WHO=Applicant SELF=N\|CN1432097 106759985 WHO=Examiner SELF=N\|US6732796 68371357 WHO=Examiner SELF=N\|US6732796 68371357 WHO=Applicant SELF=N\|US6632047 713363 WHO=Applicant SELF=N\|US6811683 48134 WHO=Applicant SELF=N\|US6543535 1439019 WHO=Examiner SELF=N\|US6543535 1439019 WHO=Applicant SELF=N\|US6543539 43300513 WHO=Examiner SELF=N\|US6543539 43300513 WHO=Applicant SELF=N\|US6485232 43276119 WHO=Applicant SELF=N\|US6824328 43394739 WHO=Applicant SELF=N\|US6419423 43252358 WHO=Examiner SELF=N\|US6419423 43252358 WHO=Applicant SELF=N\|US5997214 603718 WHO=Applicant SELF=N\|US6051137 42943979 WHO=Examiner SELF=N\|US6051137 42943979 WHO=Applicant SELF=N\|US6102622 1555459 WHO=Examiner SELF=N\|US6102622 1555459 WHO=Applicant SELF=N\|US5948253 43082999 WHO=Examiner SELF=N\|US5948253 43082999 WHO=Applicant SELF=N\|US5868202 1579437 WHO=Examiner SELF=N\|US5868202 1579437 WHO=Applicant SELF=N\|US5843214 43045633 WHO=Applicant SELF=N\|US6110359 43143044 WHO=Examiner SELF=N\|US6110359 43143044 WHO=Applicant SELF=N\|US5660500 42961429 WHO=Examiner SELF=N\|US5660500 42961429 WHO=Applicant SELF=N\|US5656239 42964545 WHO=Examiner SELF=N\|US5656239 42964545 WHO=Applicant SELF=N\|US5674424 42972644 WHO=Examiner SELF=N\|US5674424 42972644 WHO=Applicant SELF=N\|US5553189 42908634 WHO=Examiner SELF=N\|US5553189 42908634 WHO=Applicant SELF=N\|US5543041 13985117 WHO=Examiner SELF=N\|US5543041 13985117 WHO=Applicant SELF=N\|US5372621 42836640 WHO=Applicant SELF=N\|US5478443 13970508 WHO=Applicant SELF=N\|US5318116 42754267 WHO=Examiner SELF=N\|US5318116 42754267 WHO=Applicant SELF=N\|US5372708 2640335 WHO=Applicant SELF=N\|US5271693 42785257 WHO=Applicant SELF=N\|US5229583 42780625 WHO=Examiner SELF=N\|US5229583 42780625 WHO=Applicant SELF=N\|US5221827 42764654 WHO=Examiner SELF=N\|US5221827 42764654 WHO=Applicant SELF=N\|US5340467 42820083 WHO=Examiner SELF=N\|US5340467 42820083 WHO=Applicant 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SELF=N\|US4158622 60009376 WHO=Examiner SELF=N\|US4158622 60009376 WHO=Applicant SELF=N\|US4171146 42406771 WHO=Applicant SELF=N\|US4219237 42418416 WHO=Examiner SELF=N\|US4219237 42418416 WHO=Applicant SELF=N\|US4423907 42496584 WHO=Examiner SELF=N\|US4423907 42496584 WHO=Applicant SELF=N\|US4106814 60000211 WHO=Examiner SELF=N\|US4106814 60000211 WHO=Applicant SELF=N\|US4133580 42380326 WHO=Examiner SELF=N\|US4133580 42380326 WHO=Applicant SELF=N\|US4096912 42373399 WHO=Examiner SELF=N\|US4096912 42373399 WHO=Applicant SELF=N\|US4266612 3764056 WHO=Examiner SELF=N\|US4266612 3764056 WHO=Applicant SELF=N\|US4155967 42388873 WHO=Examiner SELF=N\|US4266826 42354154 WHO=Examiner SELF=N\|US4266826 42354154 WHO=Applicant SELF=N\|US4017119 42326543 WHO=Examiner SELF=N\|US4017119 42326543 WHO=Applicant SELF=N\|US3954140 42302067 WHO=Examiner SELF=N\|US3954140 42302067 WHO=Applicant SELF=N\|US4043595 42354154 WHO=Examiner SELF=N\|US4043595 42354154 WHO=Applicant SELF=N\|US4043595 42354154 WHO=Examiner SELF=N\|US4029571 1586018 WHO=Examiner SELF=N\|US4029571 1586018 WHO=Applicant SELF=N\|US3919390 42279675 WHO=Applicant SELF=N\|US3910834 3700427 WHO=Examiner SELF=N\|US3910834 3700427 WHO=Applicant SELF=N\|US3661423 2484420 WHO=Examiner SELF=N\|US3661423 2484420 WHO=Applicant SELF=N\|US3652447 42118345 WHO=Examiner SELF=N\|US3652447 42118345 WHO=Applicant SELF=N\|US3617471 95008668 WHO=Applicant SELF=N\|US2481051 41253434 WHO=Examiner SELF=N\|US2481051 41253434 WHO=Applicant SELF=N\|US1919636 40761806 WHO=Examiner SELF=N\|US1919636 40761806 WHO=Applicant SELF=N		\|WO200898177; US20080190813; US4294563; US4043595\|\|\|\|\|\|\|\|WO200898177; US20090190815; US4043595; CN1432097; US4294563; WO2008098177\|WO200898177; US20080190813; US4294563; US4043595; US4449586; WO200906687\|\|\|WO200898177; WO2008098177\|\|\|\|\|\|US4151068; US4155967; US4376107; US4449586; US20080077430; US20090007484; US4133580; US4423907; US4424021; US4717146; US4984594; US6841077; US6991033; US20070000662; US7862705; US7862706; US4430195; US5868202; US6854328; US6854929; US7004247; US7004251; US7004678; US20070023186; US3652447; US4502920; US5190405; US5193934; US4017119; US4199327; US4440446; US6051137; US6543535; US6543539; US6875356; US6881009; US7032660; US3661423; US3954140; US4266612; US4266826; US5114497; US6732796; US7040397; US7040399; US7048051; US7051811; US7534926; US4029571; US4096912; US4158622; US4452689; US4454915; US5024487; US5221827; US5318116; US6902138; US7066254; US20110138649; US1919636; US4851134; US5229583; US6419423; US6918443; US7070758; US7073578; US7077198; US7077199; US20090190813; US4043595; US4106814; US4219237; US5041209; US5137539; US5139535; US5340467; US5543041; US5656239; US5660500; US6102622; US6110359; US6923257; US6929330; US7090013; US7091460; US20080190815; US20080190816; US20080190818; US2481051; US4221648; US5244310; US5553189; US5948253; US20060213657; US3910834; US4294563; US4353418; US5674424; US1919636; US2481051; US3617471; US3652447; US3661423; US3910834; US3919390; US3954140; US4017119; US4029571; US4043595; US4096912; US4106814; US4133580; US4158622; US4171146; US4199327; US4219237; US4221648; US4234230; US4241952; US4266612; US4266826; US4294563; US4303533; US4353418; US4415365; US4423907; US4424021; US4430195; US4440446; US4452689; US4454915; US4502920; US4851134; US4879019; US4984594; US5024487; US5041209; US5076727; US5114497; US5137539; US5139535; US5190405; US5193934; US5221827; US5229583; US5244310; US5271693; US5318116; US5340467; US5372621; US5372708; US5478443; US5543041; US5553189; US5656239; US5660500; US5674424; US5843214; US5868202; US5948253; US5997214; US6051137; US6102622; US6110359; US6419423; US6485232; US6543535; US6543539; US6632047; US6732796; US6811683; US6824328; US6841077; US6854929; US6875356; US6881009; US6902138; US6918443; US6923257; US6929330; US6951247; US6962466; US6991033; US7004247; US7004251; US7004678; US7032660; US7040397; US7040399; US7048051; US7051811; US7066254; US7070758; US7073578; US7077198; US7077199; US7090013; US7091460; US7114566; US7121342; US7534926; US7862705; US7862706; KR10-0595792; JP2005306721; US20040211569; US20060213657; US20070000662; US20070023186; US20080190813; US20080190815; US20080190816; US20080190818; US20090250380; US20100200467; US20110138649; WO200898177	(EP2406351)\|Search Report references [Examiner]\|-See also references of WO 2010093777A2\|\|(US8349171)\|Applicant references\|-US Application PCT/US2010/023874; filed Feb. 11, 2010; Todd Dana; ISR mailed Oct. 13, 2010.\|-Alternative Methods for Fluid Delivery and Recovery; Manual; Sep. 1994; United States Environmental Protection Agency; 87 pgs.\|-U.S. Appl. No. 12/703,638, filed Feb. 10, 2010, Todd Dana.\|-U.S. Appl. No. 12/704,440, filed Feb. 11, 2010, Todd Dana.\|-U.S. Appl. No. 12/702,899, filed Feb. 9, 2010, Todd Dana.\|-U.S. Appl. No. 12/704,596, filed Feb. 12, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,073, filed Feb. 5, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,141, filed Feb. 5, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,156, filed Feb. 5, 2010, Todd Dana.\|-Slow Sand Filter: http://en.wikipedia.org/wiki/Slow-sand-filter; Nov. 9, 2009; 4 pages.\|-Sand Filter: http://en.wikipedia.org/wiki/Sand-filter; Nov. 9, 2009; 6 pages.\|-Related Case: U.S. Appl. No. 12/960,215, filed Dec. 3, 2010; James Patten.\|-Related Case: U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana.\|-U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana; office action issued Jun. 1, 2011.\|-PCT Application PCT/US2010/058948; filed Dec. 13, 2010; James W. Patten; International Search Report mailed Aug. 31, 2011.\|-PCT Application PCT/US2010/060854; filed Dec. 16, 2010; James W. Patten; International Search Report mailed Aug. 26, 2011.\|-U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana; Notice of Allowance issued Oct. 26, 2011.\|-U.S. Appl. No. 12/701,156, filed Feb. 5, 2010; Todd Dana; office action issued Mar. 12, 2012.\|-U.S. Appl. No. 12/701,156, filed Feb. 5, 2010; Todd Dana; notice of allowance dated Jul. 30, 2012.\|\|(WO2010/093777)\|International Search Report [Examiner]\|-See also references of EP 2406351A2\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|	GRANTED	(EP2406351)\|LAPSED\|(US8349171)\|LAPSED\|(WO2010/093777)\|LAPSED\|(CN102395653)\|LAPSED\|(VE2010000232)\|GRANTED\|(MY152426)\|GRANTED\|(MX320012)\|GRANTED\|(UA104617)\|GRANTED\|(EG26419)\|GRANTED\|(AU2010213774)\|EXPIRED\|(ZA201106555)\|GRANTED\|(MA33113)\|GRANTED\|(BRPI1008552)\|LAPSED\|(TN2011000392)\|PENDING\|(PE20120707)\|REVOKED\|(EA201171025)\|LAPSED\|(IN1891/MUMNP/2011)\|LAPSED\|(AP201105875)\|LAPSED\|(IL214550)\|LAPSED\|(CA2752133)\|LAPSED	ALIVE	(EP2406351)\|DEAD\|(US8349171)\|DEAD\|(WO2010/093777)\|DEAD\|(CN102395653)\|DEAD\|(VE2010000232)\|ALIVE\|(MY152426)\|ALIVE\|(MX320012)\|ALIVE\|(UA104617)\|ALIVE\|(EG26419)\|ALIVE\|(AU2010213774)\|DEAD\|(ZA201106555)\|ALIVE\|(MA33113)\|ALIVE\|(BRPI1008552)\|DEAD\|(TN2011000392)\|ALIVE\|(PE20120707)\|DEAD\|(EA201171025)\|DEAD\|(IN1891/MUMNP/2011)\|DEAD\|(AP201105875)\|DEAD\|(IL214550)\|DEAD\|(CA2752133)\|DEAD	(EP2406351)\|LEGAL DETAILS FOR EP2406351\|Actual or expected expiration date=2015-03-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP10741714\|Application date=2010-02-11\|Standardized application number=2010EP-0741714\|Event publication date=2011-12-16\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2012-01-18\|Event code=EP/A2\|Event group=Examination events\|Application published without search report\|Publication country=EP\|Publication number=EP2406351\|Publication stage code=A2\|Publication date=2012-01-18\|Standardized publication number=EP2406351\|Event publication date=2012-01-18\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2011-09-12\|Event publication date=2012-01-18\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR\|Event publication date=2012-05-16\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2014-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP2406351\|Publication stage code=A4\|Publication date=2014-09-17\|Standardized publication number=EP2406351\|Event publication date=2014-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2014-08-21\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2015-09-04\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2015-10-07\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2015-03-20\|(US8349171)\|LEGAL DETAILS FOR US8349171\|Actual or expected expiration date=2025-02-10\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US12703560\|Application date=2010-02-10\|Standardized application number=2010US-12703560\|Event publication date=2010-02-10\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:MCCAIG, BRIAN A\|Event publication date=2010-02-10\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1774\|Event publication date=2010-02-10\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 2488-019.NP\|Event publication date=2010-02-10\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 20551\|Event publication date=2010-02-10\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2010-02-10\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2010-03-01\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2010-03-01\|Event code=US/INCD\|Event group=Examination events OAO\|Notice Mailed--Application Incomplete--Filing Date Assigned\|Event publication date=2010-03-11\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DANA, TODD;PATTEN, JAMES W.;SIGNING DATES FROM 20090511 TO 20090623\|Reel/frame:024063/0749\|OWNER:RED LEAF RESOURCES, INC., UTAH\|Event publication date=2010-03-17\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|SECURITY AGREEMENT\|Assignors:RED LEAF RESOURCES, INC., DBA ECOSHALE AND ECOSHALE ENERGY;RED LEAF HOLDINGS, LLC;NATIONS MINING, LLC;AND OTHERS\|Reel/frame:024097/0397\|OWNER:CARDINAL ENERGY HOLDINGS, LLC, UTAH\|Effective date of the event=2009-07-02\|Event publication date=2010-04-12\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DANA, TODD;PATTEN, JAMES W.;SIGNING DATES FROM 20100317 TO 20100324\|Reel/frame:024215/0742\|OWNER:RED LEAF RESOURCES, INC., UTAH\|Event publication date=2010-04-29\|Event code=US/FLFEE\|Event group=Payment or non-payment notifications\|Payment of additional filing fee/Preexam\|Event publication date=2010-05-06\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2010-05-06\|Event code=US/POAC\|Event group=Change of name or address\|Change in Power of Attorney (May Include Associate POA)\|Event publication date=2010-05-10\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|RELEASE BY SECURED PARTY\|Assignor:CARDINAL ENERGY HOLDINGS, LLC.\|Reel/frame:024357/0626\|OWNER:RED LEAF RESOURCES, INC., D/B/A ECOSHALE, ECHOSHAL\|Effective date of the event=2010-05-07\|Event publication date=2010-05-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2010-08-12\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20100200467\|Publication stage code=A1\|Publication date=2010-08-12\|Standardized publication number=US20100200467\|Event publication date=2010-08-12\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2011-01-13\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-05-23\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-06-28\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-10-28\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-11-15\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2011-11-18\|Event code=US/DBLNF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection - Double Patenting\|RJD=2011-11-18\|R4R=DBL\|RJST=non-final\|Rejected claims 16\|RJCT=US7862705\|Event publication date=2011-11-18\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2011-11-18\|R4R=112\|RJST=non-final\|Rejected claims 1-2 and 9-11\|Event publication date=2011-11-18\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2011-11-18\|R4R=102b\|RJST=non-final\|Rejected claims 1-4 and 12; 1-5, 12-14, and 16\|RJCT=US4151068\|RJCT=US4449586\|Event publication date=2011-11-18\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2011-11-18\|R4R=102e\|RJST=non-final\|Rejected claims 1-2, 8, 12-13, and 15-16\|RJCT=US20090007484\|Event publication date=2011-11-18\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2011-11-18\|R4R=103a\|RJST=non-final\|Rejected claims 6 and 7\|RJCT=US4449586\|Event publication date=2011-12-14\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-02-21\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Action Recorded:\|RECD=2012-02-21\|Event publication date=2012-04-17\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Action Recorded:\|RECD=2012-04-17\|Event publication date=2012-04-19\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2012-04-24\|Event code=US/DBLNF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection - Double Patenting\|RJD=2012-04-24\|R4R=DBL\|RJST=non-final\|Rejected claims 16\|RJCT=US7862705\|Event publication date=2012-04-24\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2012-04-24\|R4R=102e\|RJST=non-final\|Rejected claims 16 and 17\|RJCT=US20080077430\|Event publication date=2012-04-24\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2012-04-24\|R4R=102b\|RJST=non-final\|Rejected claims 1, 3-4 and 12; 1, 3-5, 12-14, and 16\|RJCT=US4151068\|RJCT=US4449586\|Event publication date=2012-04-24\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2012-04-24\|R4R=103a\|RJST=non-final\|Rejected claims 6-8 and 15\|RJCT=US4449586\|Event publication date=2012-07-23\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-07-24\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2012-08-29\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2012-08-29\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2012-09-04\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2012-10-12\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-10-19\|Event code=US/M327\|Event group=Examination events OAO\|Miscellaneous Communication to Applicant - No Action Count\|Event publication date=2012-12-04\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2012-12-04\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2012-12-05\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2012-12-18\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2013-01-08\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US08349171\|Publication stage code=B2\|Publication date=2013-01-08\|Standardized publication number=US8349171\|Event publication date=2013-01-08\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 222 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 81 Adjustment total: \|Number of days of extension=141\|Event publication date=2016-01-19\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2016-06-15\|Event code=US/FPAY\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Fee payment recorded\|Annual fees payment date=2016-06-15\|Year of payment of annual fees=4\|Event publication date=2018-05-04\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2018-11-29\|Event code=US/M1559\|Event group=Payment or non-payment notifications\|Payment of Maintenance Fee under 1.28(c)\|Event publication date=2018-11-29\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2020-01-21\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|Event publication date=2020-05-01\|Event code=US/MAFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|Maintenance Fee Payment\|Annual fees payment date=2020-05-01\|Year of payment of annual fees=8\|PAYMENT OF MAINTENANCE FEE, 8TH YEAR, LARGE ENTITY (ORIGINAL EVENT CODE: M1552)\|Entity status of patent owner: LARGE ENTITY\|Event publication date=2020-05-01\|Event code=US/M1552\|Event group=Payment or non-payment notifications\|Payment of Maintenance Fee, 8th Year, Large Entity\|Event publication date=2024-01-23\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=11\|Event publication date=2024-08-26\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2025-01-08\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2025-01-08\|Event publication date=2025-02-10\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2025-02-10\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|(WO2010/093777)\|LEGAL DETAILS FOR WO2010/093777\|Actual or expected expiration date=2012-08-12\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2010023874\|Application date=2010-02-11\|Standardized application number=2010WO-US23874\|Event publication date=2010-08-19\|Event code=WO/A2\|Event group=Examination events\|International application published with declaration under Article 17 (2) (a)\|Publication country=WO\|Publication number=WO2010093777\|Publication stage code=A2\|Publication date=2010-08-19\|Standardized publication number=WO201093777\|Event publication date=2010-12-09\|Event code=WO/A3\|Event indicator=Pos\|Event group=Examination events\|Later publication of ISR with revised front page\|Publication country=WO\|Publication number=WO2010093777\|Publication stage code=A3\|Publication date=2010-12-09\|Standardized publication number=WO201093777\|Event publication date=2012-08-12\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AP2011005875\|Actual or expected expiration date=2016-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=AP Corresponding appl: AP201105875\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2011AP-0005875\|Corresponding cc:\|Designated or member state=AP Corresponding pat: AP2011005875\|Publication stage code in the designated or member state=A0\|Publication date in the designated or member state=2011-10-31\|Publication number in the designated or member state=AP2011005875\|Event publication date=2011-10-31\|Event code=AP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=AP\|MEMBER STATE LEGAL DETAILS FOR AU2010213774\|Actual or expected expiration date=2016-09-08\|Legal state=DEAD\|Status=EXPIRED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2010213774\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010AU-0213774\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2010213774\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2011-09-22\|Publication number in the designated or member state=AU2010213774\|Event publication date=2011-08-31\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2011-09-22\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2016-09-08\|Event code=AU/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=AU\|MEMBER STATE LEGAL DETAILS FOR BRPI1008552\|Actual or expected expiration date=2016-09-13\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BR Corresponding appl: BRPI1008552\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010BR-0008552\|Corresponding cc:\|Designated or member state=BR Corresponding pat: BRPI1008552\|Publication stage code in the designated or member state=A0\|Publication date in the designated or member state=2012-11-20\|Publication number in the designated or member state=BR201008552\|Event publication date=2012-11-20\|Event code=WO/REG\|Event code=BR/B01A\|Event group=Examination events\|Reference to a national code\|Pct publication - request for entry into the national phase\|Comunicacao da publicacao internacional pct. apresentacao de peticao de requerimento de entrada na fase nacional\|Corresponding cc:\|Designated or member state=BR\|Event publication date=2016-03-15\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2011-08-12\|Corresponding cc:\|Designated or member state=BR\|Event publication date=2017-01-10\|Event code=BR/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=BR\|MEMBER STATE LEGAL DETAILS FOR CA2752133\|Actual or expected expiration date=2016-02-11\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA2752133\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010CA-2752133\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA2752133\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2010-08-19\|Publication number in the designated or member state=CA2752133\|Event publication date=2011-08-10\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CA\|Event publication date=2016-03-24\|Event code=CA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR CL\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=CL Corresponding appl: CL2011001975\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CL\|MEMBER STATE LEGAL DETAILS FOR CN102395653\|Actual or expected expiration date=2016-02-11\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN201080016465\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010CN-80016465\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN102395653\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-03-28\|Publication number in the designated or member state=CN102395653\|Event publication date=2010-02-11\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CN\|Event publication date=2017-03-29\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2011-08-12\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2011-08-12\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR DZ\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=DZ Corresponding appl: DZDZP2011000592\|Event publication date=2011-09-08\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=DZ\|MEMBER STATE LEGAL DETAILS FOR EA201171025\|Actual or expected expiration date=2017-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EA Corresponding appl: EA201171025\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2011EA-0071025\|Corresponding cc:\|Designated or member state=EA Corresponding pat: EA201171025\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2012-02-28\|Publication number in the designated or member state=EA201171025\|Event publication date=2011-09-08\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EA\|Event publication date=2012-02-28\|Event code=EA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EA\|MEMBER STATE LEGAL DETAILS FOR EG26419\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=EG Corresponding appl: EG2011081356\|Application date in the designated or member state=2011-08-11\|Application number in the designated or member state=2011EG-0081356\|Corresponding cc:\|Designated or member state=EG Corresponding pat: EG26419\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2013-10-23\|Publication number in the designated or member state=EG--26419\|Event publication date=2013-10-23\|Event code=EG/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EG\|MEMBER STATE LEGAL DETAILS FOR EP2406351\|Actual or expected expiration date=2015-03-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP10741714\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010EP-0741714\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2406351\|Publication stage code in the designated or member state=A2\|Publication date in the designated or member state=2012-01-18\|Publication number in the designated or member state=EP2406351\|Event publication date=2010-10-06\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2011-09-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2015-10-07\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR GE\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=GE Corresponding appl: GE12376\|Event publication date=2011-09-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=GE\|MEMBER STATE LEGAL DETAILS FOR IL214550\|Actual or expected expiration date=2016-09-27\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IL Corresponding appl: IL214550\|Application date in the designated or member state=2011-02-11\|Application number in the designated or member state=2011IL-0214550\|Corresponding cc:\|Designated or member state=IL Corresponding pat: IL214550\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-09-27\|Publication number in the designated or member state=IL-214550\|Event publication date=2011-08-09\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IL\|Event publication date=2011-09-27\|Event code=IL/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IL\|MEMBER STATE LEGAL DETAILS FOR IN1891/MUMNP/2011\|Actual or expected expiration date=2022-02-03\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN1891/MUMNP/2011\|Application date in the designated or member state=2011-09-09\|Application number in the designated or member state=2011IN-MN01891\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN1891/MUMNP/2011\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-02-03\|Publication number in the designated or member state=IN2011MN01891\|Event publication date=2011-09-09\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|Event publication date=2012-02-03\|Event code=IN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IN\|MEMBER STATE LEGAL DETAILS FOR MA33113\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=MA Corresponding appl: MA34158\|Application date in the designated or member state=2011-09-09\|Application number in the designated or member state=2011MA-0034158\|Corresponding cc:\|Designated or member state=MA Corresponding pat: MA33113\|Publication stage code in the designated or member state=B1\|Publication date in the designated or member state=2012-03-01\|Publication number in the designated or member state=MA--33113\|Event publication date=2012-03-01\|Event code=MA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=MA\|MEMBER STATE LEGAL DETAILS FOR MX2011008534\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=MX Corresponding appl: MX2011008534\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2011MX-0008534\|Corresponding cc:\|Designated or member state=MX Corresponding pat: MX2011008534\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-12-16\|Publication number in the designated or member state=MX2011008534\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=MX\|Event publication date=2014-05-05\|Event code=MX/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=MX\|MEMBER STATE LEGAL DETAILS FOR PE\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=PE Corresponding appl: PE001479-2011\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=PE\|MEMBER STATE LEGAL DETAILS FOR TN2011000392\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=TN Corresponding appl: TN2011000392\|Application date in the designated or member state=2011-08-09\|Application number in the designated or member state=2011TN-0000392\|Corresponding cc:\|Designated or member state=TN Corresponding pat: TN2011000392\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2013-03-27\|Publication number in the designated or member state=TN2011000392\|MEMBER STATE LEGAL DETAILS FOR UA104617\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=UA Corresponding appl: UAA201110794\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2011UA-0010794\|Corresponding cc:\|Designated or member state=UA Corresponding pat: UA104617\|Publication stage code in the designated or member state=C2\|Publication date in the designated or member state=2014-02-25\|Publication number in the designated or member state=UA-104617\|Event publication date=2014-02-25\|Event code=UA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=UA\|MEMBER STATE LEGAL DETAILS FOR ZA201106555\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=ZA Corresponding appl: ZA201106555\|Application date in the designated or member state=2011-09-07\|Application number in the designated or member state=2011ZA-0006555\|Corresponding cc:\|Designated or member state=ZA Corresponding pat: ZA201106555\|Publication stage code in the designated or member state=B\|Publication date in the designated or member state=2012-05-30\|Publication number in the designated or member state=ZA201106555\|Event publication date=2012-05-30\|Event code=ZA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=ZA\|(CN102395653)\|LEGAL DETAILS FOR CN102395653\|Actual or expected expiration date=2016-02-11\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201080016465\|Application date=2010-02-11\|Standardized application number=2010CN-80016465\|Event publication date=2012-03-28\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN102395653\|Publication stage code=A\|Publication date=2012-03-28\|Standardized publication number=CN102395653\|Event publication date=2012-03-28\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2012-05-09\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2015-05-06\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN102395653\|Publication stage code=B\|Publication date=2015-05-06\|Standardized publication number=CN102395653B\|Event publication date=2015-05-06\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2017-03-29\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee\|Effective date of the event=2016-02-11\|(VE2010000232)\|LEGAL DETAILS FOR VE2010000232\|Actual or expected expiration date=2030-02-12\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-12\|Event code=VE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=VE VE2010-000232\|Application date=2010-02-12\|Standardized application number=2010VE-0000232\|Event publication date=2012-07-26\|Event code=VE/A\|Event indicator=Pos\|Event group=Examination events\|Patent Application or Foreign Patent Application\|Publication country=VE\|Publication number=VE2010000232\|Publication stage code=A\|Publication date=2012-07-26\|Standardized publication number=VE2010000232\|Event publication date=2021-12-13\|Event code=VE/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted National or Foreign Invention Patent\|Publication country=VE\|Publication number=VE2010000232\|Publication stage code=B\|Publication date=2021-12-13\|Standardized publication number=VE2010000232\|(MY152426)\|LEGAL DETAILS FOR MY152426\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-11\|Event code=MY/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MY MYPI2011003744\|Application date=2010-02-11\|Standardized application number=2011MY-0003744\|Event publication date=2014-09-30\|Event code=MY/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent / Utility Model\|Publication country=MY\|Publication number=MY152426\|Publication stage code=A\|Publication date=2014-09-30\|Standardized publication number=MY-152426\|(MX320012)\|LEGAL DETAILS FOR MX320012\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-11\|Event code=MX/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MX MX2011008534\|Application date=2010-02-11\|Standardized application number=2011MX-0008534\|Event publication date=2011-12-16\|Event code=MX/A\|Event group=Examination events\|Patent application\|Publication country=MX\|Publication number=MX2011008534\|Publication stage code=A\|Publication date=2011-12-16\|Standardized publication number=MX2011008534\|Event publication date=2014-05-05\|Event code=MX/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent/ granted utility model\|Publication country=MX\|Publication number=MX320012\|Publication stage code=B\|Publication date=2014-05-05\|Standardized publication number=MX-320012\|Event publication date=2014-05-05\|Event code=MX/FG\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant or registration\|Concesion\|(UA104617)\|LEGAL DETAILS FOR UA104617\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-11\|Event code=UA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=UA UAA201110794\|Application date=2010-02-11\|Standardized application number=2011UA-0010794\|Event publication date=2014-02-25\|Event code=UA/C2\|Event indicator=Pos\|Event group=Event indicating In Force\|Pat. grant. upon the USSR appl.,for which no pos. dec. made;grant. upon basis of national application\|Publication country=UA\|Publication number=UA104617\|Publication stage code=C2\|Publication date=2014-02-25\|Standardized publication number=UA-104617\|(EG26419)\|LEGAL DETAILS FOR EG26419\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-08-11\|Event code=EG/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EG EG2011081356\|Application date=2011-08-11\|Standardized application number=2011EG-0081356\|Event publication date=2013-10-23\|Event code=EG/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent for invention / Patent of addition\|Publication country=EG\|Publication number=EG26419\|Publication stage code=A\|Publication date=2013-10-23\|Standardized publication number=EG--26419\|(AU2010213774)\|LEGAL DETAILS FOR AU2010213774\|Actual or expected expiration date=2016-09-08\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=2010-02-11\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2010213774\|Application date=2010-02-11\|Standardized application number=2010AU-0213774\|Event publication date=2011-09-22\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2010213774\|Publication stage code=A1\|Publication date=2011-09-22\|Standardized publication number=AU2010213774\|Event publication date=2013-06-13\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent proceeded by OPI\|Publication country=AU\|Publication number=AU2010213774\|Publication stage code=B2\|Publication date=2013-06-13\|Standardized publication number=AU2010213774\|Event publication date=2013-10-10\|Event code=AU/FGA\|Event indicator=Pos\|Event group=Event indicating In Force\|Letters patent sealed or granted (standard patent)\|Event publication date=2016-09-08\|Event code=AU/MK14\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent ceased section 143(a) (annual fees not paid) or expired\|(ZA201106555)\|LEGAL DETAILS FOR ZA201106555\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-09-07\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA201106555\|Application date=2011-09-07\|Standardized application number=2011ZA-0006555\|Event publication date=2012-05-30\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA201106555\|Publication stage code=B\|Publication date=2012-05-30\|Standardized publication number=ZA201106555\|(MA33113)\|LEGAL DETAILS FOR MA33113\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-09-09\|Event code=MA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MA MA34158\|Application date=2011-09-09\|Standardized application number=2011MA-0034158\|Event publication date=2012-03-01\|Event code=MA/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=MA\|Publication number=MA33113\|Publication stage code=B1\|Publication date=2012-03-01\|Standardized publication number=MA--33113\|(BRPI1008552)\|LEGAL DETAILS FOR BRPI1008552\|Actual or expected expiration date=2016-09-13\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=BR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=BR BRPI1008552\|Application date=2010-02-11\|Standardized application number=2010BR-0008552\|Event publication date=2012-11-20\|Event code=BR/A0\|Event indicator=Pos\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=BR\|Publication number=BRPI1008552\|Publication stage code=A0\|Publication date=2012-11-20\|Standardized publication number=BR201008552\|Event publication date=2016-03-15\|Event code=BR/A2\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention / pipeline patent published without search report\|Publication country=BR\|Publication number=BRPI1008552\|Publication stage code=A2\|Publication date=2016-03-15\|Standardized publication number=BR201008552\|Event publication date=2016-09-13\|Event code=BR/B08F\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application fees: dismissal - article 86 of industrial property law\|Anuidade do pedido: arquivamento . Art. 86 da lpi [codigo 8.6 rpi]\|REFERENTE A 6A ANUIDADE.\|Event publication date=2017-01-10\|Event code=BR/B08K\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Lapse as no evidence of payment of the annual fee has been furnished to inpi (acc. art. 87)\|Manutencao do arquivamento [codigo 8.11 rpi]\|EM VIRTUDE DO ARQUIVAMENTO PUBLICADO NA RPI 2384 DE 13-09-2016 E CONSIDERANDO AUSENCIA DE MANIFESTACAO DENTRO DOS PRAZOS LEGAIS, INFORMO QUE CABE SER MANTIDO O ARQUIVAMENTO DO PEDIDO DE PATENTE, CONFORME O DISPOSTO NO ARTIGO 12, DA RESOLUCAO 113/2013.\|(TN2011000392)\|LEGAL DETAILS FOR TN2011000392\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2011-08-09\|Event code=TN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=TN TN2011000392\|Application date=2011-08-09\|Standardized application number=2011TN-0000392\|Event publication date=2013-03-27\|Event code=TN/A1\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention\|Publication country=TN\|Publication number=TN2011000392\|Publication stage code=A1\|Publication date=2013-03-27\|Standardized publication number=TN2011000392\|(PE20120707)\|LEGAL DETAILS FOR PE20120707\|Actual or expected expiration date=2016-01-29\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2010-02-11\|Event code=PE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=PE PE2011001479\|Application date=2010-02-11\|Standardized application number=2011PE-0001479\|Event publication date=2012-06-27\|Event code=PE/A1\|Event group=Examination events\|Patent application\|Publication country=PE\|Publication number=PE20120707\|Publication stage code=A1\|Publication date=2012-06-27\|Standardized publication number=PE201200707\|Event publication date=2016-01-29\|Event code=PE/FC\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Refusal\|Rechazada o denegada\|(EA201171025)\|LEGAL DETAILS FOR EA201171025\|Actual or expected expiration date=2017-02-28\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=EA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EA EA201171025\|Application date=2010-02-11\|Standardized application number=2011EA-0071025\|Event publication date=2012-02-28\|Event code=EA/A1\|Event group=Examination events\|Public. of applic. with search report\|Publication country=EA\|Publication number=EA201171025\|Publication stage code=A1\|Publication date=2012-02-28\|Standardized publication number=EA201171025\|Event publication date=2017-02-28\|Event code=EA/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IN1891/MUMNP/2011)\|LEGAL DETAILS FOR IN1891/MUMNP/2011\|Actual or expected expiration date=2022-02-03\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-09-09\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN1891/MUMNP/2011\|Application date=2011-09-09\|Standardized application number=2011IN-MN01891\|Event publication date=2012-02-03\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN1891/MUMNP/2011\|Publication stage code=A\|Publication date=2012-02-03\|Standardized publication number=IN2011MN01891\|Event publication date=2022-02-03\|Event code=IN/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(AP201105875)\|LEGAL DETAILS FOR AP201105875\|Actual or expected expiration date=2016-10-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=AP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AP AP201105875\|Application date=2010-02-11\|Standardized application number=2011AP-0005875\|Event publication date=2011-10-31\|Event code=AP/D0\|Event indicator=Pos\|Event group=Examination events\|Patent application filed\|Publication country=AP\|Publication number=AP201105875\|Publication stage code=D0\|Publication date=2011-10-31\|Standardized publication number=AP201105875\|Event publication date=2011-10-31\|Event code=AP/A0\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=AP\|Publication number=AP2011005875\|Publication stage code=A0\|Publication date=2011-10-31\|Standardized publication number=AP2011005875\|Event publication date=2016-10-31\|Event code=AP/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IL214550)\|LEGAL DETAILS FOR IL214550\|Actual or expected expiration date=2016-09-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-02-11\|Event code=IL/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IL IL214550\|Application date=2011-02-11\|Standardized application number=2011IL-0214550\|Event publication date=2011-09-27\|Event code=IL/A\|Event group=Examination events\|Application of patent for invention\|Publication country=IL\|Publication number=IL214550\|Publication stage code=A\|Publication date=2011-09-27\|Standardized publication number=IL-214550\|Event publication date=2016-09-27\|Event code=IL/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(CA2752133)\|LEGAL DETAILS FOR CA2752133\|Actual or expected expiration date=2016-02-11\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2752133\|Application date=2010-02-11\|Standardized application number=2010CA-2752133\|Event publication date=2010-08-19\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2752133\|Publication stage code=A1\|Publication date=2010-08-19\|Standardized publication number=CA2752133\|Event publication date=2016-03-24\|Event code=CA/FZDE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Dead\|Effective date of the event=2016-02-11	(EP2406351)\|Contracting States: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2010/093777)\|ARIPO: GH, GM, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2010/093777)\|EAPO: RU, TJ, BY, MD, AZ, TM, AM, KG, KZ\|(WO2010/093777)\|EPO: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2010/093777)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2010/093777)\|National States: PT, HN, HR, HU, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KM, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PE, PG, PH, PL	(WO2010/093777)\|CL; DZ; EG; GE; MA; MX; PE; TN; UA; ZA\|(VE2010000232)\|VE\|(MY152426)\|MY\|(MX320012)\|MX\|(UA104617)\|UA\|(EG26419)\|EG\|(ZA201106555)\|ZA\|(MA33113)\|MA\|(TN2011000392)\|TN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=jP3Nqvhw8TiycRSLnaM7OHmXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US8349171&ekey=948&xpn=EP2406351&kind=A4	https://register.epo.org/application?number=EP10741714	https://permalink.orbit.com/RenderStaticFirstPage?XPN=xq6OlXDbYJMuw56Xk6cpNXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2010/093777)\|US\|(US8349171)\|US	(WO2010/093777)\|NAME=RED LEAF RESOURCES, INC. 200 W. Civic Center Drive, Suite 190, Sandy, UT 84070 , COUNTRY=US\|(US8349171)\|NAME=Red Leaf Resources, Inc. , CITY=Sandy , STATE=UT , COUNTRY=US , ATYP=US Company	(EP2406351)\|DE\|(EP2406351)\|DE\|\|(US20100200467)\|US\|(WO2010/093777)\|US\|\|\|\|\|\|\|(AU2010213774)\|AU\|(AU2010213774)\|AU\|(CA2752133)\|CA	(EP2406351)\|NAME=Walker, Ross Thomson;Forresters Skygarden Erika-Mann-Strasse 11 , CITY=80636 München , COUNTRY=DE , REG=101298687\|(EP2406351)\|NAME=Walker, Ross Thomson;Forrester & Boehmert Pettenkoferstrasse 20-22 , CITY=80336 München , COUNTRY=DE , REG=100045009\|(US8349171)\|NAME=Thorpe North & Western LLP\|(US20100200467)\|NAME=THORPE NORTH & WESTERN, LLP. P.O. Box 1219 , CITY=SANDY , STATE=UT , POSTCODE=84091-1219 , COUNTRY=US\|(WO2010/093777)\|NAME=Ericksen Erik S. et al. Thorpe North & Western, LLP, Po Box 1219, Sandy, UT 84091-1219 , COUNTRY=US\|(CN102395653)\|NAME=ZHAO RONGMIN;JEEKAI & PARTNERS , REG=11245\|(CN102395653)\|NAME=ZHAO RONGMIN;JEEKAI & PARTNERS , REG=11245\|(VE2010000232)\|NAME=LINARES ALLOCA MARLIN ENEIDA\|(VE2010000232)\|NAME=LINARES ALLOCA MARLIN ENEIDA\|(MX320012)\|NAME=MARIA ANGELICA PARDAVELL JUAREZ\|(MX2011008534)\|NAME=MARIA ANGELICA PARDAVELL JUAREZ\|(AU2010213774)\|NAME=FB Rice Level 23 44 Market Street , CITY=SYDNEY , STATE=NSW , POSTCODE=2000 , COUNTRY=AU\|(AU2010213774)\|NAME=FB Rice Level 23 44 Market Street , CITY=Sydney , STATE=NSW , POSTCODE=2000 , COUNTRY=AU\|(CA2752133)\|NAME=BERESKIN & PARR LLP/S.E.N.C.R.L.,S.R.L. , COUNTRY=CA	(EP2406351)\|US; US\|(EP2406351)\|US; US\|(US8349171)\|US; US\|(US20100200467)\|US; US\|\|(WO2010/093777)\|US; US\|\|\|\|\|(MX320012)\|US; US\|\|\|\|\|\|\|\|\|\|\|(IN1891/MUMNP/2011)\|US; US\|\|(CA2752133)\|US; US	(EP2406351)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, CITY=Park CityUT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., CITY=SandyUT 84092, COUNTRY=US\|(EP2406351)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, CITY=Park CityUT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., CITY=SandyUT 84092, COUNTRY=US\|(US8349171)\|NAME=Dana Todd, CITY=Park City, STATE=UT , COUNTRY=US \|NAME=Patten James W., CITY=Sandy, STATE=UT , COUNTRY=US\|(US20100200467)\|NAME=Dana Todd, CITY=Park City, STATE=UT , COUNTRY=US \|NAME=Patten James W., CITY=Sandy, STATE=UT , COUNTRY=US\|(WO2010/093777)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(WO2010/093777)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, Park City, UT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., Sandy, UT 84092, COUNTRY=US\|(CN102395653)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(CN102395653)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(VE2010000232)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(MY152426)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES W.\|(MX320012)\|NAME=TODD DANA, COUNTRY=US \|NAME=JAMES W PATTEN, COUNTRY=US\|(MX2011008534)\|NAME=TODD DANA\|NAME=JAMES W PATTEN\|(UA104617)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(EG26419)\|NAME=DANA TODD 3473 W. Daybreaker Drive Park City, UT 84098-US)\|NAME=PATTEN JAMES W 4216 E. Wildcreek Rd. Sandy, UT 84092-US\|(AU2010213774)\|NAME=Dana, Todd\|NAME=Patten, James W.\|(AU2010213774)\|NAME=Dana, Todd\|NAME=Patten, James W.\|(ZA201106555)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(MA33113)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(BRPI1008552)\|NAME=JAMES W. PATTEN 4216 E.WILDCREEK RD SANDY UT US - 84092 US\|NAME=TODD DANA 3473 W. DAYBREAKER DRIVE PARK CITY UT US-84098 US\|(TN2011000392)\|NAME=PATTEN JAMES W.\|NAME=DANA TODD\|(PE20120707)\|NAME=PATTEN, JAMES W.\|NAME=DANA, TODD\|(IN1891/MUMNP/2011)\|NAME=TODD DANA, COUNTRY=US \|NAME=PATTEN JAMES W, COUNTRY=US\|(AP2011005875)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(CA2752133)\|NAME=DANA, TODD, COUNTRY=US \|NAME=PATTEN, JAMES W., COUNTRY=US	(IN1891/MUMNP/2011)\|5\|(CN102395653)\|5\|(AU2010213774)\|5\|(CA2752133)\|5\|(US8349171)\|5	3	20		CARDINAL ENERGY HOLDINGS; FROM 2009-07-02; TO 2010-05-07	(EP2406351)\|WO2010/093777\|(CN102395653)\|WO2010/093777\|(MX320012)\|WO2010/093777\|(UA104617)\|WO2010/093777\|(EG26419)\|WO2010/093777\|(AU2010213774)\|WO2010/093777\|(ZA201106555)\|WO2010/093777\|(MA33113)\|WO2010/093777\|(BRPI1008552)\|WO2010/093777\|(TN2011000392)\|WO2010/093777\|(EA201171025)\|WO2010/093777\|(IN1891/MUMNP/2011)\|WO2010/093777\|(AP201105875)\|WO2010/093777\|(IL214550)\|WO2010/093777\|(CA2752133)\|WO2010/093777		Primary examiner: Pardo Torre, J\|\|Primary examiner: Pardo Torre, J\|\|(US8349171)\|Number of Claims: NCL=17\|Number of Drawings: NDR=5\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1,16\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=141\|Primary examiner: McCaig Brian\|Art Unit.: ART =1774\|\|(US20100200467)\|Number of Claims: NCL=16\|Number of Drawings: NDR=5\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1,16\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: McCaig Brian\|Art Unit.: ART =1774\|\|(WO2010/093777)\|Number of Claims: NCL=16\|Extended kind: EXTK=z\|\|(CN102395653)\|Number of Claims: NCL=18\|Gazette date: GAZDATE=2015-05-06\|Gazette number: GAZNUM=31-18\|Substantial examination effective date: 20120509 Examination duration: 35 months\|Number of Pages: NPAGES=25\|Primary examiner: Zhou Shuge\|Primary examiner: 周淑歌\|\|(CN102395653)\|Number of Claims: NCL=16\|Gazette date: GAZDATE=2012-03-28\|Gazette number: GAZNUM=28-13\|Substantial examination effective date: 20120509 Examination duration: 35 months\|Number of Pages: NPAGES=24\|Primary examiner: Zhou Shuge\|Primary examiner: 周淑歌\|\|(MX2011008534)\|Number of Claims: NCL=16\|Number of Pages: NPAGES=88\|\|(AU2010213774)\|Number of Claims: NCL=17\|\|(AU2010213774)\|Number of Claims: NCL=16\|\|(IN1891/MUMNP/2011)\|Number of Claims: NCL=16\|\|(AP2011005875)\|Gazette date: GAZDATE=2011-10-31\|\|(CA2752133)\|Number of Claims: NCL=16\|Number of Pages: NPAGES=45\|	(US8349171)\|Provisional Appl: US61/152,146 FDD=2009-02-12 [2009US-61152146]\|Previous publication: US20100200467 A1 2010-08-12 [US20100200467]	(EP2406351)\|ENGLISH (ENG)	(VE2010000232)\|Patent\|(BR201008552)\|Patent\|(CN102395653B)\|Patent\|(MY-152426)\|Patent\|(EP2406351)\|Patent\|(MX-320012)\|Patent\|(UA-104617)\|Patent\|(EG--26419)\|Patent\|(AU2010213774)\|Patent\|(TN2011000392)\|Patent\|(US8349171)\|Patent\|(BR201008552)\|Patent\|(VE2010000232)\|Patent\|(PE201200707)\|Patent\|(ZA201106555)\|Patent\|(CN102395653)\|Patent\|(MA--33113)\|Patent\|(EA201171025)\|Patent\|(IN2011MN01891)\|Patent\|(EP2406351)\|Patent\|(MX2011008534)\|Patent\|(AP2011005875)\|Patent\|(AP201105875)\|Patent\|(IL-214550)\|Patent\|(AU2010213774)\|Patent\|(WO201093777)\|Patent\|(CA2752133)\|Patent\|(WO201093777)\|Patent\|(US20100200467)\|Patent	Titre: (EP2406351)\|Methods of recovering hydrocarbons from hydrocarbonaceous material using a constructed infrastructure and associated systems maintained under positive pressure Résumé: (EP2406351)\|A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure (100). This constructed infrastructure (100) defines a substantially encapsulated volume. A comminuted hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body (120) of hydrocarbonaceous material. The permeable body (120) can be heated sufficient to remove hydrocarbons therefrom. During heating and removal of hydrocarbons and subsequent thereto a positive pressure can be maintained within the encapsulated volume by means of a non-oxidizing gas to expedite flushing of hydrocarbonaceous material, inhibit unwanted entry of oxygen into the encapsulated volume and remove recoverable hydrocarbons following the heating process.	45	Abstract	gpt-4o-mini	no	The article focuses on recovering hydrocarbons from hydrocarbonaceous materials and does not mention accelerated weathering, CO₂ capture, or related processes.
43	US63/203,814P\|US63/203,814\|US17/815,914\|WOIB2022/057088\|US18/302,702\|US18/673,248	US18/673,248\|US18/302,702\|WOIB2022/057088\|IN202417013808\|EP22848809\|JP2024505303\|BR112024001825\|AU2022318480\|CA3227505\|US17/815,914	US12545576\|EP4377258\|US20240308843\|JP2024528907\|US12006212\|EP4377258\|BR112024001825\|IN202417013808\|AU2022318480\|BR112024001825\|US20230271827\|US20230102312\|CA3227505\|WO2023/007466	104224295	US12545576 B2 2026-02-10 [US12545576]\|US20240308843 A1 2024-09-19 [US20240308843]\|US12006212 B2 2024-06-11 [US12006212]\|US20230271827 A1 2023-08-31 [US20230271827]\|WO2023/007466 A1 2023-02-02 [WO202307466]\|IN202417013808 A 2024-03-15 [IN202417013808]\|EP4377258 A4 2025-09-17 [EP4377258]\|EP4377258 A1 2024-06-05 [EP4377258]\|JP2024528907 A 2024-08-01 [JP2024528907]\|BR112024001825 A2 2024-04-24 [BR112024001825]\|BR112024001825 A0 2024-02-06 [BR112024001825]\|AU2022318480 A1 2024-02-22 [AU2022318480]\|CA3227505 A1 2023-02-02 [CA3227505]\|US20230102312 A1 2023-03-30 [US20230102312]	2021-07-30\|2022-07-28\|2022-07-29\|2023-04-18\|2024-05-23	2024-05-23\|2023-04-18\|2022-07-29\|2024-02-26\|2022-07-29\|2022-07-29\|2022-07-29\|2022-07-29\|2022-07-29\|2022-07-28	2026-02-10\|2025-09-17\|2024-09-19\|2024-08-01\|2024-06-11\|2024-06-05\|2024-04-24\|2024-03-15\|2024-02-22\|2024-02-06\|2023-08-31\|2023-03-30\|2023-02-02\|2023-02-02	\|(US12545576)\|2026-02-10\|(US12006212)\|2024-06-11\|\|\|\|\|\|\|	(EP4377258)\|2042-07-29\|(US12545576)\|2042-07-28\|(US12006212)\|2042-07-28\|(US20230102312)\|2023-06-09\|(WO2023/007466)\|2025-01-30\|(JP2024528907)\|2026-03-09\|(BR112024001825)\|2042-07-29\|(IN202417013808)\|2042-07-29\|(AU2022318480)\|2042-07-29\|(CA3227505)\|2042-07-29	(EP4377258)\|Systems and methods for generating hydrogen and magnetite from rock	(EP4377258)\|Systems and methods for sequestering carbon, evolving hydrogen gas, producing iron oxide as magnetite, and producing magnesium carbonate as magnesite through sequential carbonation and serpentinization/hydration reactions involving processed olivine- and/or pyroxene-rich ores, as typically found in mafic and ultramafic igneous rock. Precious or scarce metals, such nickel, cobalt, chromium, rare earth elements, and others, may be concentrated in the remaining ore to facilitate their recovery from any gangue material.	FOUNDATION OHIO STATE INNOVATION\|OHIO STATE INNOVATION FOUNDATION	(EP4377258)\|Ohio State Innovation Foundation\|(EP4377258)\|Ohio State Innovation Foundation ([US])\|(US12545576)\|Ohio State Innovation Foundation ([US])\|(US20240308843)\|Ohio State Innovation Foundation ([US])\|(US12006212)\|Ohio State Innovation Foundation ([US])\|(US20230271827)\|Ohio State Innovation Foundation ([US])\|(US20230102312)\|Ohio State Innovation Foundation ([US])\|(WO2023/007466)\|OHIO STATE INNOVATION FOUNDATION ([US])\|(JP2024528907)\|OHIO STATE INNOVATION FOUNDATION\|(BR112024001825)\|FOUNDATION OHIO STATE INNOVATION ([US])\|\|(IN202417013808)\|OHIO STATE INNOVATION FOUNDATION\|(AU2022318480)\|OHIO STATE INNOVATION FOUNDATION\|(CA3227505)\|OHIO STATE INNOVATION FOUNDATION ([US])	DARRAH THOMAS\|RAO VIKRAM\|WHYTE COLIN	(EP4377258)\|DARRAH, Thomas\|RAO, Vikram\|WHYTE, Colin\|(EP4377258)\|DARRAH, Thomas\|RAO, Vikram\|WHYTE, Colin	(EP4377258)\|K&L Gates LLP;Karolinen Karree ([DE])\|Reg. Nb: 101744768\|(US12545576)\|K&L Gates LLP\|(US12006212)\|K&L Gates LLP\|(WO2023/007466)\|EASWARAN, David ([US])\|(JP2024528907)\|KIMURA, Mitsuru\|Reg. Nb: 100095407\|Yasushi Morikawa\|Reg. Nb: 100132883\|Kei Sakurada\|Reg. Nb: 100148633\|Hide Mie\|Reg. Nb: 100147924\|(AU2022318480)\|K&L Gates ([AU])\|(CA3227505)\|ROWAND LLP ([CA])	(US12545576)\|It will be appreciated that the scope of the present disclosure encompasses many potential embodiments in addition to those summarized above, some of which will be described in further detail below.\|Conversely, hydrogen formation in a more conventional manner, such as by natural gas reforming, is limited by natural gas availability, among other constraints that are often carbon intensive.\|Instead, natural systems, which evolve through time and under varying reaction conditions produce complex (and often heterogeneous) complexes of varying mineral assemblages and products of reactions that did not follow the idealized reactions described above, or are slower to reach thermodynamic equilibrium.\|Such reactions produce variable and complex mineralogy and chemistry but do not predictably produce any specific combination of reaction products.\|	(US12545576)\|1. A system for sequestering carbon and producing hydrogen and magnetite from rock, the system comprising: a source of ore containing olivine or pyroxene; a reactor having an inlet that receives ore particles and at least one outlet, the reactor also having at least one additional inlet through which one or more of carbon dioxide or water is introduced, the reactor operable at a first temperature for a first residence time to react carbon dioxide that enters the reactor through the at least one additional inlet with the ore particles to generate magnesium carbonate, the reactor also operable at a second temperature for a second residence time to react water that enters the reactor through the at least one additional inlet with the ore particles to generate magnetite and hydrogen gas; and a gas separator that is connected to and in fluid communication with the at least one outlet of the reactor, the gas separator configured to separate hydrogen gas from gases that exit the reactor through the at least one outlet.\|18. A method for generating hydrogen and magnetite from rock, the method comprising: obtaining an ore containing olivine or pyroxene; introducing the ore into a reactor that is operable at temperatures above ambient temperature and pressures above atmospheric pressure; introducing water into the reactor at a particular temperature for a particular residence time to react with the ore to generate magnetite and hydrogen gas; removing, from the reactor, a gas mixture that includes the hydrogen gas; separating the hydrogen gas from the gas mixture; and removing any remaining ore from the reactor.\|	(US12545576)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|The disclosure herein provides one or more embodiments of systems and methods for sequestering carbon, evolving hydrogen gas, and producing magnetite as well as magnesite from olivine- and pyroxene-bearing ores.\|The disclosure herein provides one or more embodiments of systems and methods that facilitate the production of hydrogen, magnetite, and/or other desired minerals through serpentinization reactions involving olivine- and pyroxene-rich ores generally found in mafic and/or ultramafic igneous rock, or of any other rock assemblages containing such olivine- and pyroxene-rich ores.\|	(US12545576)\|MAGNETITE(100,58)\|ROCK(100,32)\|ORE PARTICLE(100,12)\|HYDROGEN GENERATION(100,6)\|REACTOR(77,124)\|MAFIC IGNEOUS ROCK(63,7)\|ROCK ASSEMBLAGE(59,1)\|ULTRAMAFIC IGNEOUS ROCK(58,7)\|PYROXENE RICH ORE(55,16)\|SEQUESTERING CARBON(51,6)\|REMAINING ORE PARTICLE(46,3)\|THERMODYNAMIC EQUILIBRIUM(44,2)\|OLIVINE(42,31)\|ORE(41,36)\|MINERAL ASSEMBLAGE(38,2)\|COMPLEX MINERALOGY(38,1)\|SERPENTINIZATION REACTION(33,23)\|GANGUE MINERAL(32,2)\|SEQUENTIAL CARBONATION(31,5)\|REMAINING ORE(30,16)\|GAS SEPARATOR(29,11)\|PYROXENE BEARING ORE(29,3)\|PRESELECTED SIZE(28,7)\|MAGNETIC SEPARATOR(27,7)\|PYROXENE(26,18)\|SCARCE METAL PRODUCTION(25,1)\|MAGNESITE(24,29)\|CARBON INTENSIVE(23,2)\|CARBON DIOXIDE(22,66)\|SCARCE METAL(22,15)\|CARBON DIOXIDE MINERALIZATION(22,5)\|PRODUCING MAGNETITE(22,4)\|HYDROGEN FORMATION(22,1)\|NATURAL GAS REFORMING(22,1)\|NATURAL GAS AVAILABILITY(20,1)\|CRUSHER(19,6)\|FLUID COMMUNICATION(19,3)\|HYDROGEN GAS(18,47)\|COMMINUTING(18,1)\|SIEVE(17,9)\|MAGNESIUM CARBONATE PRODUCTION(17,1)\|ROCK POWDER(16,6)\|CHEMISTRY(16,2)\|MAGNESIUM CARBONATE(15,31)\|PRECIOUS METAL(15,8)\|CHROMIUM(15,6)\|FORSTERITE MINERAL(15,4)\|GAS MIXTURE(15,2)\|COBALT(14,8)\|AMBIENT TEMPERATURE(14,4)\|COMMINUTED ROCK(14,4)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|PATHWAY(13,7)\|REACTION PRODUCT(12,22)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|DESIRED MINERAL(12,1)\|IRON OXIDE PRODUCTION(12,1)\|INORGANIC PHASE(11,13)\|UNREACTED ROCK ORE(11,3)\|GANGUE MATERIAL(11,2)\|WEATHERED MINERAL MINING(11,1)\|HYDROGEN PRODUCTION(10,13)\|CRUSHED GROUND ROCK(10,6)\|WASHER(10,3)\|NEUTRALIZE ACIDIFICATION(10,2)\|YOUNG OCEANIC CRUST(10,2)\|FAYALITE PRECONCENTRATION(10,1)\|FAYALITE SERPENTINIZATION(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|ECONOMIC VIABILITY(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|MAFIC IGNEOUS ROCK POTENTIAL(9,1)\|MAFIC ULTRAMAFIC ORE(9,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(9,1)\|MINERAL GRAIN COMMINUTION(9,1)\|SERPENTINIZATION REACTIONSSERPENTINIZATION REACTION(9,1)\|RESIDENCE TIME(8,21)\|SUPERCRITICAL CARBON DIOXIDE(8,3)\|UNREACTED ORE ROCK(8,2)\|CARBON MINERALIZATION KINETICS(8,1)\|HOMOGENIZED OLIVINE(8,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(8,1)\|OLIVINE ABUNDANCE(8,1)\|ORE CARBONATION DRIVEN COMMINUTION(8,1)\|PYROXENE MINERALOGY(8,1)\|RELEVANT CONSTITUENT ABUNDANCE(8,1)\|REVENUE ENTITLEMENT(8,1)\|ROCK DRIVER COMMINUTION(8,1)\|SERPENTINIZATION REACTION REACTIVITY(8,1)\|SERPENTINIZED ULTRAMAFIC ROCK(8,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(8,1)\|RARE EARTH ELEMENT(7,9)\|ATMOSPHERIC PRESSURE(7,6)\|CARBON NEUTRAL(7,6)\|COPPER BED(7,3)\|SEQUESTER CARBON DIOXIDE(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|BAND HEATER(7,2)\|BATCH EXPERIMENT(7,2)\|CERAMIC BRICK(7,2)\|FRACTIONATION FACTOR(7,2)\|GEOLOGICAL SITE(7,2)\|MAGNETITE MAGNESITE PRODUCTION(7,2)\|PYROLYSIS REACTION(7,2)\|RELEVANT COMPONENT(7,2)\|ROUGH PUMP(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|RESIDUAL IRON SILICATE(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBON DIOXIDE MINERALIZATION KINETICS(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|OLIVINE MINERAL PHASE(6,1)\|OLIVINE RICH DEPOSIT(6,1)\|OLIVINE RICH ORC(6,1)\|OLIVINE RICH ORE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|ALUMINUM OXIDE(5,9)\|REACTION CONDITION(5,6)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION(5,1)\|CIRCUMNEUTRAL PH(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|COPPER FILING HEATED BED(5,1)\|CRYOGENIC SEPARATION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL LATTICE(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE TEST(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REACTIONSDECARBONATION REACTION(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SIO DENSITY SEPARATION(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,25)\|HEAVY LIQUID SEPARATION(4,5)\|CARBON DIOXIDE GAS(4,4)\|MGCO(4,4)\|MGO(4,4)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE REACTIVITY(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|ENHANCE CARBON DIOXIDE SEQUESTRATION(4,2)\|ENHANCING PRODUCTION(4,2)\|IRON SILICATE PHASE(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|TAX CREDIT(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|COMMENSURATE CARBON DIOXIDE SEQUESTRATION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|INSOLUBLE MAGNESIUM CARBONATE(4,1)\|IRON RICH MINERAL(4,1)\|IRON SILICATE MINERAL PHASE(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM CARBONATE BULK(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE LOCATION(4,1)\|OLIVINEFAYALITE(4,1)\|OLIVINEFORSTERITEMG(4,1)\|PROCESSED ROCK(4,1)\|PYROXENEENSTATITEMG(4,1)\|PYROXENEFERROSILITE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|WATER OXYGEN FUGACITY(4,1)\|STOICHIOMETRIC RATIO(3,4)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SULFUR DIOXIDE(3,3)\|FLOWCHART BLOCK(3,2)\|FOSSIL FUEL COMBUSTION(3,2)\|STEAM METHANE REFORMING(3,2)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|DECADE(3,1)\|DISSOLUTION(3,1)\|ENHANCING CARBON DIOXIDE SEQUESTRATION(3,1)\|EXCESS UNREACTED CARBON DIOXIDE(3,1)\|EXPANSION VOLUME(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GASEOUS CARBON DIOXIDE(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|INCREASED MINERALIZATION(3,1)\|REACHING RESERVE(3,1)\|\|(US20240308843)\|MAGNETITE(100,58)\|ROCK(100,32)\|HYDROGEN PRODUCTION(100,13)\|ORE PARTICLE(100,12)\|HYDROGEN GENERATION(100,6)\|SEQUESTERING CARBON(100,6)\|REACTOR(75,123)\|MAGNESITE SEQUENTIAL CARBONATION(74,1)\|MAFIC IGNEOUS ROCK(63,7)\|ROCK ASSEMBLAGE(59,1)\|ULTRAMAFIC IGNEOUS ROCK(58,7)\|PYROXENE RICH ORE(55,16)\|REMAINING ORE PARTICLE(53,4)\|ORE(44,38)\|THERMODYNAMIC EQUILIBRIUM(44,2)\|OLIVINE(41,34)\|MINERAL ASSEMBLAGE(38,2)\|COMPLEX MINERALOGY(38,1)\|COMMINUTING(35,2)\|SERPENTINIZATION REACTION(34,25)\|REMAINING ORE(30,15)\|GAS SEPARATOR(30,11)\|PYROXENE BEARING ORE(29,3)\|PRESELECTED SIZE(28,7)\|MAGNETIC SEPARATOR(27,7)\|PYROXENE(26,20)\|SCARCE METAL PRODUCTION(25,1)\|CARBON INTENSIVE(23,2)\|SCARCE METAL(22,15)\|CARBON DIOXIDE MINERALIZATION(22,5)\|PRODUCING MAGNETITE(22,4)\|HYDROGEN FORMATION(22,1)\|NATURAL GAS REFORMING(22,1)\|CARBON DIOXIDE(21,90)\|MAGNESITE(21,28)\|NATURAL GAS AVAILABILITY(20,1)\|CRUSHER(19,6)\|FLUID COMMUNICATION(19,3)\|MAGNESIUM CARBONATE(18,35)\|SIEVE(17,9)\|SUPERCRITICAL CARBON DIOXIDE(17,3)\|HYDROGEN GAS(16,46)\|ROCK POWDER(16,6)\|CHEMISTRY(16,2)\|CHROMIUM(15,6)\|FORSTERITE MINERAL(15,4)\|COBALT(14,8)\|AMBIENT TEMPERATURE(14,4)\|COMMINUTED ROCK(14,4)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|PATHWAY(13,7)\|PRECIOUS METAL(13,7)\|REACTION PRODUCT(12,22)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|DESIRED MINERAL(12,1)\|UNREACTED ROCK ORE(11,3)\|GANGUE MATERIAL(11,2)\|DECARBONATION IGNEOUS MOLE(11,1)\|WEATHERED MINERAL MINING(11,1)\|CRUSHED GROUND ROCK(10,6)\|WASHER(10,3)\|NEUTRALIZE ACIDIFICATION(10,2)\|YOUNG OCEANIC CRUST(10,2)\|FAYALITE PRECONCENTRATION(10,1)\|FAYALITE SERPENTINIZATION(10,1)\|OLIVINE RICH ORC(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|ECONOMIC VIABILITY(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|MAFIC IGNEOUS ROCK POTENTIAL(9,1)\|MAFIC ULTRAMAFIC ORE(9,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(9,1)\|MINERAL GRAIN COMMINUTION(9,1)\|OLIVINE RICH DEPOSIT(9,1)\|OLIVINE RICH ORE(9,1)\|RESIDENCE TIME(8,21)\|UNREACTED ORE ROCK(8,2)\|CARBON MINERALIZATION KINETICS(8,1)\|GASEOUS CO2 DISSOLUTION(8,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(8,1)\|OLIVINE ABUNDANCE(8,1)\|ORE CARBONATION DRIVEN COMMINUTION(8,1)\|PYROXENE MINERALOGY(8,1)\|RELEVANT CONSTITUENT ABUNDANCE(8,1)\|REVENUE ENTITLEMENT(8,1)\|ROCK DRIVER COMMINUTION(8,1)\|SEQUESTRATION TAX CREDIT(8,1)\|SERPENTINIZATION REACTION REACTIVITY(8,1)\|SERPENTINIZED ULTRAMAFIC ROCK(8,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(8,1)\|RARE EARTH ELEMENT(7,9)\|ATMOSPHERIC PRESSURE(7,6)\|CARBON NEUTRAL(7,6)\|COPPER BED(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|BAND HEATER(7,2)\|BATCH EXPERIMENT(7,2)\|CERAMIC BRICK(7,2)\|FRACTIONATION FACTOR(7,2)\|GEOLOGICAL SITE(7,2)\|MAGNETITE MAGNESITE PRODUCTION(7,2)\|PYROLYSIS REACTION(7,2)\|RELEVANT COMPONENT(7,2)\|ROUGH PUMP(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STEAM METHANE REFORMING REACTION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|SUPERCRITICAL CO2(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|MGCO3(5,6)\|REACTION CONDITION(5,6)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|FE2SI2O(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CIRCUMNEUTRAL PH(5,1)\|CO2 MINERALIZATION RATE(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|COPPER FILING HEATED BED(5,1)\|CRYOGENIC SEPARATION(5,1)\|DECARBONATION REACTION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,25)\|SMALL SIZE FRACTION(4,6)\|HEAVY LIQUID SEPARATION(4,5)\|SODIUM BICARBONATE(4,5)\|FE3O(4,4)\|H2O(4,4)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|ENHANCING PRODUCTION(4,2)\|INORGANIC PHASE REACTION(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|MG2SIO(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|WATER OXYGEN FUGACITY(4,1)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|FLOWCHART BLOCK(3,2)\|FOSSIL FUEL COMBUSTION(3,2)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|DECADE(3,1)\|ENHANCING CARBON DIOXIDE(3,1)\|EXPANSION VOLUME(3,1)\|FE2SIO(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|INTENDED CARBONATION REACTION(3,1)\|REACHING RESERVE(3,1)\|\|(US12006212)\|REACTOR(100,131)\|MAGNETITE(100,58)\|ROCK(100,33)\|HYDROGEN(100,27)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,5)\|ORE(86,53)\|MAGNESITE SEQUENTIAL CARBONATION(77,1)\|MAFIC IGNEOUS ROCK(65,7)\|REMAINING ORE(61,19)\|ROCK ASSEMBLAGE(61,1)\|ULTRAMAFIC IGNEOUS ROCK(60,7)\|PYROXENE RICH ORE(58,16)\|COPPER FILING HEATED BED(52,3)\|OLIVINE(47,34)\|THERMODYNAMIC EQUILIBRIUM(46,2)\|COPPER FILING(45,3)\|WATER OXYGEN FUGACITY(44,3)\|OXYGEN FUGACITY(43,13)\|MINERAL ASSEMBLAGE(40,2)\|COMPLEX MINERALOGY(40,1)\|RECTOR(40,1)\|SERPENTINIZATION REACTION(34,23)\|PYROXENE(33,20)\|ORE PARTICLE(33,5)\|PRESELECTED SIZE(32,8)\|HEATED BED(32,3)\|AMBIENT TEMPERATURE(31,6)\|ACIDIC SOLUTION(30,4)\|PYROXENE BEARING ORE(30,3)\|MAGNESIUM CARBONATE(27,38)\|COMMINUTING(27,2)\|SUPERCRITICAL CARBON DIOXIDE(26,4)\|SCARCE METAL PRODUCTION(26,1)\|CARBON DIOXIDE(25,92)\|CARBON INTENSIVE(24,2)\|SCARCE METAL(23,15)\|CARBON DIOXIDE MINERALIZATION(23,5)\|PRODUCING MAGNETITE(23,4)\|HYDROGEN FORMATION(23,1)\|NATURAL GAS REFORMING(23,1)\|MAGNESITE(22,28)\|HYDROGEN GAS(21,48)\|NATURAL GAS AVAILABILITY(21,1)\|CHROMIUM(16,6)\|ROCK POWDER(16,6)\|CHEMISTRY(16,2)\|ATMOSPHERIC PRESSURE(15,8)\|COBALT(15,8)\|FORSTERITE MINERAL(15,4)\|PATHWAY(14,7)\|PRECIOUS METAL(14,7)\|COMMINUTED ROCK(14,4)\|OLIVINE RICH ORE(14,2)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|REACTION PRODUCT(13,22)\|INORGANIC PHASE(13,16)\|DESIRED MINERAL(13,1)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|WEATHERED MINERAL MINING(12,1)\|CRUSHED GROUND ROCK(11,6)\|UNREACTED ROCK ORE(11,3)\|GANGUE MATERIAL(11,2)\|LITHIUM(11,2)\|NEUTRALIZE ACIDIFICATION(11,2)\|YOUNG OCEANIC CRUST(11,2)\|FAYALITE PRECONCENTRATION(11,1)\|FAYALITE SERPENTINIZATION(11,1)\|RESIDENCE TIME(10,20)\|GAS SEPARATOR(10,9)\|MAGNETIC SEPARATOR(10,5)\|ECONOMIC VIABILITY(10,2)\|MAFIC IGNEOUS ROCK POTENTIAL(10,1)\|MAFIC ULTRAMAFIC ORE(10,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(10,1)\|MINERAL GRAIN COMMINUTION(10,1)\|OLIVINE RICH DEPOSIT(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|SIEVE(8,7)\|CARBON NEUTRAL(8,6)\|UNREACTED ORE ROCK(8,2)\|CARBON MINERALIZATION KINETICS(8,1)\|GASEOUS CO2 DISSOLUTION(8,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(8,1)\|MINERAL IGNEOUS MOLE(8,1)\|OLIVINE ABUNDANCE(8,1)\|ORE CARBONATION DRIVEN COMMINUTION(8,1)\|PYROXENE MINERALOGY(8,1)\|RELEVANT CONSTITUENT ABUNDANCE(8,1)\|REVENUE ENTITLEMENT(8,1)\|SEQUESTRATION TAX CREDIT(8,1)\|SERPENTINIZATION REACTION REACTIVITY(8,1)\|SERPENTINIZED ULTRAMAFIC ROCK(8,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(8,1)\|RARE EARTH ELEMENT(7,9)\|COPPER BED(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|BAND HEATER(7,2)\|BATCH EXPERIMENT(7,2)\|CERAMIC BRICK(7,2)\|CO2 MINERALIZATION RATE(7,2)\|FRACTIONATION FACTOR(7,2)\|GEOLOGICAL SITE(7,2)\|MAGNETITE MAGNESITE PRODUCTION(7,2)\|PYROLYSIS REACTION(7,2)\|RELEVANT COMPONENT(7,2)\|ROUGH PUMP(7,2)\|SUPERCRITICAL CO2(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STEAM METHANE REFORMING REACTION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|CRUSHER(6,4)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|MGCO3(5,6)\|REACTION CONDITION(5,6)\|HEAVY LIQUID SEPARATION(5,5)\|SODIUM BICARBONATE(5,5)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|CRYOGENIC SEPARATION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,25)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|ENHANCING PRODUCTION(4,2)\|FE2SI2O(4,2)\|FE2SIO(4,2)\|FLUID COMMUNICATION(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|MG2SIO(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PHASE DECARBONATION REACTION(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|HYDROGEN PRODUCTION(3,12)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|FLOWCHART BLOCK(3,2)\|FOSSIL FUEL COMBUSTION(3,2)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|DECADE(3,1)\|ENHANCING CARBON DIOXIDE(3,1)\|EXPANSION VOLUME(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|REACHING RESERVE(3,1)\|\|(US20230271827)\|REACTOR(100,132)\|MAGNETITE(100,60)\|ROCK(100,33)\|HYDROGEN(100,26)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,5)\|MAGNESITE SEQUENTIAL CARBONATION(78,1)\|ORE(76,50)\|ORE PARTICLE(71,9)\|REMAINING ORE(68,21)\|MAFIC IGNEOUS ROCK(66,7)\|ROCK ASSEMBLAGE(62,1)\|ULTRAMAFIC IGNEOUS ROCK(61,7)\|PYROXENE RICH ORE(58,16)\|OLIVINE(47,34)\|THERMODYNAMIC EQUILIBRIUM(46,2)\|MINERAL ASSEMBLAGE(40,2)\|COMPLEX MINERALOGY(40,1)\|COPPER FILING HEATED BED(39,3)\|PRESELECTED SIZE(38,10)\|SERPENTINIZATION REACTION(35,23)\|PYROXENE(34,20)\|WATER OXYGEN FUGACITY(34,3)\|GAS SEPARATOR(32,11)\|ACIDIC SOLUTION(30,4)\|PYROXENE BEARING ORE(30,3)\|MAGNETIC SEPARATOR(28,7)\|MAGNESIUM CARBONATE(27,38)\|COMMINUTING(27,2)\|SCARCE METAL PRODUCTION(27,1)\|CARBON DIOXIDE(25,92)\|SCARCE METAL(24,15)\|AMBIENT TEMPERATURE(24,5)\|CARBON INTENSIVE(24,2)\|CARBON DIOXIDE MINERALIZATION(23,5)\|PRODUCING MAGNETITE(23,4)\|HYDROGEN FORMATION(23,1)\|NATURAL GAS REFORMING(23,1)\|MAGNESITE(22,28)\|HYDROGEN GAS(21,48)\|NATURAL GAS AVAILABILITY(21,1)\|CRUSHER(20,6)\|FLUID COMMUNICATION(20,3)\|SIEVE(18,9)\|SUPERCRITICAL CARBON DIOXIDE(18,3)\|ROCK POWDER(17,6)\|CHROMIUM(16,6)\|CHEMISTRY(16,2)\|COBALT(15,8)\|FORSTERITE MINERAL(15,4)\|PATHWAY(14,7)\|PRECIOUS METAL(14,7)\|COMMINUTED ROCK(14,4)\|OLIVINE RICH ORE(14,2)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|REACTION PRODUCT(13,22)\|INORGANIC PHASE(13,16)\|DESIRED MINERAL(13,1)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|GANGUE MATERIAL(12,2)\|WEATHERED MINERAL MINING(12,1)\|ATMOSPHERIC PRESSURE(11,7)\|CRUSHED GROUND ROCK(11,6)\|UNREACTED ROCK ORE(11,3)\|LITHIUM(11,2)\|NEUTRALIZE ACIDIFICATION(11,2)\|YOUNG OCEANIC CRUST(11,2)\|FAYALITE PRECONCENTRATION(11,1)\|FAYALITE SERPENTINIZATION(11,1)\|RESIDENCE TIME(10,20)\|ECONOMIC VIABILITY(10,2)\|MAFIC IGNEOUS ROCK POTENTIAL(10,1)\|MAFIC ULTRAMAFIC ORE(10,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(10,1)\|MINERAL GRAIN COMMINUTION(10,1)\|OLIVINE RICH DEPOSIT(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|CARBON MINERALIZATION KINETICS(9,1)\|GASEOUS CO2 DISSOLUTION(9,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(9,1)\|MINERAL IGNEOUS MOLE(9,1)\|OLIVINE ABUNDANCE(9,1)\|ORE CARBONATION DRIVEN COMMINUTION(9,1)\|PYROXENE MINERALOGY(9,1)\|RELEVANT CONSTITUENT ABUNDANCE(9,1)\|REVENUE ENTITLEMENT(9,1)\|SEQUESTRATION TAX CREDIT(9,1)\|SERPENTINIZATION REACTION REACTIVITY(9,1)\|SERPENTINIZED ULTRAMAFIC ROCK(9,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(9,1)\|CARBON NEUTRAL(8,6)\|BAND HEATER(8,2)\|BATCH EXPERIMENT(8,2)\|CERAMIC BRICK(8,2)\|CO2 MINERALIZATION RATE(8,2)\|ENHANCED IMPLEMENTED ACCOUNTING(8,2)\|FRACTIONATION FACTOR(8,2)\|GEOLOGICAL SITE(8,2)\|MAGNETITE MAGNESITE PRODUCTION(8,2)\|PYROLYSIS REACTION(8,2)\|RELEVANT COMPONENT(8,2)\|ROUGH PUMP(8,2)\|UNREACTED ORE ROCK(8,2)\|RARE EARTH ELEMENT(7,9)\|COPPER BED(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|SUPERCRITICAL CO2(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STEAM METHANE REFORMING REACTION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|REACTION CONDITION(6,6)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|MGCO3(5,6)\|HEAVY LIQUID SEPARATION(5,5)\|SODIUM BICARBONATE(5,5)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CIRCUMNEUTRAL PH(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|CRYOGENIC SEPARATION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,25)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|FE2SI2O(4,2)\|FE2SIO(4,2)\|FLOWCHART BLOCK(4,2)\|FOSSIL FUEL COMBUSTION(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|MG2SIO(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PHASE DECARBONATION REACTION(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|COPPER ALLOY EFFORT(3,1)\|DECADE(3,1)\|EXPANSION VOLUME(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|INTENDED CARBONATION REACTION(3,1)\|IRON ORE NATURE(3,1)\|IRON RICH IRON ORE(3,1)\|IRON SILICATE MINERAL PHASE(3,1)\|KILOGRAM(3,1)\|LANTHANUM(3,1)\|REACHING RESERVE(3,1)\|\|(US20230102312)\|MAGNETITE(100,60)\|ROCK(100,33)\|HYDROGEN(100,26)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,5)\|REACTOR(99,134)\|MAGNESITE SEQUENTIAL CARBONATION(78,1)\|ORE(76,50)\|ORE PARTICLE(71,9)\|REMAINING ORE(68,21)\|MAFIC IGNEOUS ROCK(66,7)\|ROCK ASSEMBLAGE(62,1)\|ULTRAMAFIC IGNEOUS ROCK(61,7)\|PYROXENE RICH ORE(58,16)\|OLIVINE(47,35)\|THERMODYNAMIC EQUILIBRIUM(46,2)\|MINERAL ASSEMBLAGE(41,2)\|COPPER FILING HEATED BED(40,3)\|COMPLEX MINERALOGY(40,1)\|PRESELECTED SIZE(38,10)\|SERPENTINIZATION REACTION(35,23)\|PYROXENE(34,20)\|WATER OXYGEN FUGACITY(34,3)\|GAS SEPARATOR(31,12)\|ACIDIC SOLUTION(30,4)\|PYROXENE BEARING ORE(30,3)\|MAGNETIC SEPARATOR(28,7)\|MAGNESIUM CARBONATE(27,38)\|COMMINUTING(27,2)\|SCARCE METAL PRODUCTION(27,1)\|CARBON DIOXIDE(25,92)\|SCARCE METAL(24,15)\|AMBIENT TEMPERATURE(24,5)\|CARBON INTENSIVE(24,2)\|CARBON DIOXIDE MINERALIZATION(23,5)\|PRODUCING MAGNETITE(23,4)\|HYDROGEN FORMATION(23,1)\|NATURAL GAS REFORMING(23,1)\|MAGNESITE(22,28)\|HYDROGEN GAS(21,48)\|FLUID COMMUNICATION(21,3)\|NATURAL GAS AVAILABILITY(21,1)\|CRUSHER(20,6)\|SIEVE(18,9)\|SUPERCRITICAL CARBON DIOXIDE(18,3)\|ROCK POWDER(17,6)\|CHROMIUM(16,6)\|CHEMISTRY(16,2)\|COBALT(15,8)\|FORSTERITE MINERAL(15,4)\|PATHWAY(14,7)\|PRECIOUS METAL(14,7)\|COMMINUTED ROCK(14,4)\|OLIVINE RICH ORE(14,2)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|REACTION PRODUCT(13,22)\|INORGANIC PHASE(13,16)\|DESIRED MINERAL(13,1)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|GANGUE MATERIAL(12,2)\|WEATHERED MINERAL MINING(12,1)\|ATMOSPHERIC PRESSURE(11,7)\|CRUSHED GROUND ROCK(11,6)\|UNREACTED ROCK ORE(11,3)\|LITHIUM(11,2)\|NEUTRALIZE ACIDIFICATION(11,2)\|YOUNG OCEANIC CRUST(11,2)\|FAYALITE PRECONCENTRATION(11,1)\|FAYALITE SERPENTINIZATION(11,1)\|RESIDENCE TIME(10,20)\|ECONOMIC VIABILITY(10,2)\|MAFIC IGNEOUS ROCK POTENTIAL(10,1)\|MAFIC ULTRAMAFIC ORE(10,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(10,1)\|MINERAL GRAIN COMMINUTION(10,1)\|OLIVINE RICH DEPOSIT(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|CARBON MINERALIZATION KINETICS(9,1)\|GASEOUS CO2 DISSOLUTION(9,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(9,1)\|MINERAL IGNEOUS MOLE(9,1)\|OLIVINE ABUNDANCE(9,1)\|ORE CARBONATION DRIVEN COMMINUTION(9,1)\|OUTCROP QUARRYING(9,1)\|PYROXENE MINERALOGY(9,1)\|RELEVANT CONSTITUENT ABUNDANCE(9,1)\|REVENUE ENTITLEMENT(9,1)\|SEQUESTRATION TAX CREDIT(9,1)\|SERPENTINIZATION REACTION REACTIVITY(9,1)\|SERPENTINIZED ULTRAMAFIC ROCK(9,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(9,1)\|CARBON NEUTRAL(8,6)\|BAND HEATER(8,2)\|BATCH EXPERIMENT(8,2)\|CERAMIC BRICK(8,2)\|CO2 MINERALIZATION RATE(8,2)\|CRYOGENIC SEPARATION(8,2)\|FRACTIONATION FACTOR(8,2)\|GEOLOGICAL SITE(8,2)\|MAGNETITE MAGNESITE PRODUCTION(8,2)\|PYROLYSIS REACTION(8,2)\|RELEVANT COMPONENT(8,2)\|ROUGH PUMP(8,2)\|UNREACTED ORE ROCK(8,2)\|RARE EARTH ELEMENT(7,9)\|COPPER BED(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|SUPERCRITICAL CO2(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|GRAVITY SEPARATION(6,9)\|REACTOR VESSEL(6,9)\|REACTION CONDITION(6,6)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|TOROIDAL FLUIDIZED BED(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|REACTION STEP(5,29)\|HEAVY LIQUID SEPARATION(5,6)\|MGCO3(5,6)\|SODIUM BICARBONATE(5,5)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|SOURCE ROCK COMMINUTION(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CIRCUMNEUTRAL PH(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ROTARY KILN(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|FE2SI2O(4,2)\|FE2SIO(4,2)\|FLOWCHART BLOCK(4,2)\|FOSSIL FUEL COMBUSTION(4,2)\|MAGNESIUM COMPONENT(4,2)\|MG2SIO(4,2)\|STEAM METHANE REFORMING(4,2)\|TAILING(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PHASE DECARBONATION REACTION(4,1)\|POLLEN(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|VALENCE(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|MEMBRANE SEPARATION(3,3)\|PRELIMINARY RESULT(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|DECADE(3,1)\|EXPANSION VOLUME(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|INTENDED CARBONATION REACTION(3,1)\|IRON ORE NATURE(3,1)\|IRON RICH IRON ORE(3,1)\|IRON SILICATE MINERAL PHASE(3,1)\|KILOGRAM(3,1)\|REACHING RESERVE(3,1)\|\|(WO2023/007466)\|REACTOR(100,176)\|MAGNETITE(100,64)\|ROCK(100,34)\|HYDROGEN(100,25)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,7)\|H DROGEN(100,1)\|ORE(69,64)\|REMAINING ORE(69,31)\|ORE PARTICLE(57,11)\|MAGNESITE SEQUENTIAL CARBONATION(54,1)\|MAFIC IGNEOUS ROCK(45,7)\|ROCK ASSEMBLAGE(43,1)\|ULTRAMAFIC IGNEOUS ROCK(42,7)\|PYROXENE RICH ORE(40,16)\|OLIVINE(36,35)\|COMMINUTING(36,6)\|COPPER FILING HEATED BED(34,4)\|THERMODYNAMIC EQUILIBRIUM(32,2)\|RESIDENCE RIME(32,1)\|PRESELECTED SIZE(31,13)\|ACIDIC SOLUTION(31,7)\|WATER OXYGEN FUGACITY(29,4)\|PYROXENE BEARING ORE(29,3)\|CARBON DIOXIDE(28,113)\|PYROXENE(28,20)\|MINERAL ASSEMBLAGE(28,2)\|COMPLEX MINERALOGY(28,1)\|SERPENTINIZATION REACTION(24,24)\|AMBIENT TEMPERATURE(22,6)\|GAS SEPARATOR(21,12)\|MAGNESIUM CARBONATE(20,39)\|CHROMIUM(19,9)\|MAGNETIC SEPARATOR(19,7)\|SUPERCRITICAL CARBON DIOXIDE(19,3)\|SCARCE METAL PRODUCTION(18,1)\|HYDROGEN GAS(17,50)\|COBALT(17,11)\|CARBON INTENSIVE(17,2)\|SCARCE METAL(16,16)\|CARBON DIOXIDE MINERALIZATION(16,5)\|PRODUCING MAGNETITE(16,4)\|HYDROGEN FORMATION(16,1)\|NATURAL GAS REFORMING(16,1)\|MAGNESITE(15,29)\|CRUSHER(14,5)\|FLUID COMMUNICATION(14,3)\|NATURAL GAS AVAILABILITY(14,1)\|VAIYING REACTION CONDITION(14,1)\|RESIDENCE TIME(12,37)\|SIEVE(12,9)\|ROCK POWDER(11,6)\|LITHIUM(11,3)\|CHEMISTRY(11,2)\|ATMOSPHERIC PRESSURE(10,8)\|PATHWAY(10,7)\|COMMINUTED ROCK(10,4)\|FORSTERITE MINERAL(10,4)\|IMMENSE GEOLOGICAL SCALABILITY(10,1)\|REACTION PRODUCT(9,22)\|INORGANIC PHASE(9,17)\|PRECIOUS METAL(9,7)\|OLIVINE RICH ORE(9,2)\|DESIRED MINERAL(9,1)\|RARE EARTH ELEMENT(8,12)\|CARBON SEQUESTRATION(8,9)\|CARBONIZATION REACTION(8,5)\|UNREACTED ROCK ORE(8,3)\|GANGUE MATERIAL(8,2)\|WEATHERED MINERAL MINING(8,1)\|YOUNG OCEANIC CMST(8,1)\|CRUSHED GROUND ROCK(7,6)\|WASHER(7,3)\|ECONOMIC VIABILITY(7,2)\|NEUTRALIZE ACIDIFICATION(7,2)\|FAYALITE PRECONCENTRATION(7,1)\|FAYALITE SERPENTINIZATION(7,1)\|MAFIC IGNEOUS ROCK POTENTIAL(7,1)\|MAFIC ULTRAMAFIC ORE(7,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(7,1)\|MINERAL GRAIN COMMINUTION(7,1)\|OLIVINE RICH DEPOSIT(7,1)\|SUPERCRITICAL CAIBON DIOXIDE(7,1)\|ACCESSORY MINERAL COLLECTION(6,3)\|THERMOCOUPLE DETECTOR(6,3)\|AGGREGATE SUBSTITUTE(6,2)\|FERROSILITE MINERAL PHASE(6,2)\|MAFIC IGNEOUS ROCK SOURCE(6,2)\|PULVERIZED ROCK(6,2)\|RESIDUAL GANGUE(6,2)\|UNREACTED ORE ROCK(6,2)\|CARBON MINERALIZATION KINETICS(6,1)\|GASEOUS CO2 DISSOLUTION(6,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(6,1)\|OLIVINE ABUNDANCE(6,1)\|ORE CARBONATION DRIVEN COMMINUTION(6,1)\|OUTCROP QUARRYING(6,1)\|PYROXENE MINERALOGY(6,1)\|RELEVANT CONSTITUENT ABUNDANCE(6,1)\|REVENUE ENTITLEMENT(6,1)\|SEQUESTRATION TAX CREDIT(6,1)\|SERPENTINIZATION REACTION REACTIVITY(6,1)\|SERPENTINIZED ULTRAMAFIC ROCK(6,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(6,1)\|SMALL SIZE FRACTION(5,10)\|CARBON NEUTRAL(5,6)\|SRI GAS CHROMATOGRAPH(5,3)\|BAND HEATER(5,2)\|BATCH EXPERIMENT(5,2)\|CERAMIC BRICK(5,2)\|CRYOGENIC SEPARATION(5,2)\|FRACTIONATION FACTOR(5,2)\|GEOLOGICAL SITE(5,2)\|MAGNETITE MAGNESITE PRODUCTION(5,2)\|PYROLYSIS REACTION(5,2)\|RELEVANT COMPONENT(5,2)\|REMAINING ROCK GANGUE(5,2)\|ROUGH PUMP(5,2)\|ABIOGENIC METHANE FORMATION(5,1)\|CARBON MINERALIZATION EXPERIMENT(5,1)\|COMMINUTED ORE(5,1)\|EARTH CONTINENTAL CRUST(5,1)\|ECONOMIC GEOLOGICAL HYDROGEN(5,1)\|FORSTERITE AVAILABILITY(5,1)\|GANGUE MINERAL(5,1)\|GASEOUS CAIBON REACTION(5,1)\|HOMOGENIZED OLIVINE(5,1)\|HYDROGEN EVOLUTION KINETICS(5,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(5,1)\|NONCONDENSABLE FRACTION(5,1)\|REMAINING BULK ROCK GEOCHEMICAL(5,1)\|ROCK ORE BREAKDOWN(5,1)\|SCALABLE MAGNESITE(5,1)\|SCIENTIFIC SUPPLIER(5,1)\|SEQUENTIAL CARBONIZATION(5,1)\|STOICHIOMETRIC ASSESSMENT(5,1)\|STOICHIOMETRIC MODELING(5,1)\|ULTRAMAFRC ROCK(5,1)\|UNREACTED FAYALITE(5,1)\|YOUNG OCEANIC CRUST(5,1)\|GRAVITY SEPARATION(4,9)\|REACTOR VESSEL(4,9)\|FERTILIZER(4,4)\|PRESELECTED TEMPERATURE(4,4)\|ROTARY KILN(4,4)\|STANDARD OMEGA(4,4)\|ACCOUNTING(4,3)\|DIHYDROGEN SULFIDE(4,3)\|ELECTRICITY(4,3)\|EVEN CARBON NEGATIVE(4,3)\|IRON RICH SILICATE MINERAL(4,3)\|LANDFILL(4,3)\|NATURAL REACTION(4,3)\|REMAINING ROCK ORE(4,3)\|SEQUENTIAL REACTION(4,3)\|SOURCE ROCK COMMINUTION(4,3)\|VALUABLE CONSTITUENT(4,3)\|COMPETITION(4,2)\|COPPER BED(4,2)\|OLIVINE WASTE STREAM(4,2)\|OMEGA K WIRE THERMOCOUPLE(4,2)\|RESIDUAL GAS ANALYZER(4,2)\|AGGREGATE SALE(4,1)\|AMBIENT OXYGEN FUGACITY(4,1)\|CARBONATE MINERALIZATION(4,1)\|COMMENSURATE LY(4,1)\|ENABLED EXPERIMENTATION(4,1)\|ENSTATITE MINERAL(4,1)\|GOVERNMENT MANDATED REGULATION(4,1)\|MAGNETITE RECOVERY(4,1)\|MID OCEANIC RIDGE(4,1)\|MINERAL BREAKDOWN(4,1)\|MITIGATE ATMOSPHERIC RELEASE(4,1)\|PROLIFIC OCCURRENCE(4,1)\|QUARRYING CONCEPT(4,1)\|REACTION SEQUENTIAL ORDERING(4,1)\|ROCK HAMMER(4,1)\|ROCK METRIC TON(4,1)\|SEQUENTIAL SERPENTINIZATION REACTION(4,1)\|STEAM REFORMER(4,1)\|STOICHIOMETRIC CALCULATION(4,1)\|THERMOCHEMICAL DRIVER(4,1)\|TOROIDAL FLUIDIZED BED(4,1)\|ULTRAMAFIC ROCK BULK SAMPLE(4,1)\|REACTION STEP(3,29)\|HEAVY LIQUID SEPARATION(3,6)\|SODIUM BICARBONATE(3,5)\|POTASSIUM HYDROXIDE(3,4)\|PSI PRESSURE GAUGE(3,4)\|ACCESSORY MINERAL PHASE(3,2)\|AGRICULTURAL LIME(3,2)\|BRUCITE(3,2)\|CARBON DIOXIDE INTRODUCTION(3,2)\|CRUSHING(3,2)\|ELECTROLYSIS(3,2)\|MAGNESIUM COMPONENT(3,2)\|MAGNETITE REACTION PRODUCT(3,2)\|TAILING(3,2)\|ULTRAMAFIC AGGREGATE MATERIAL(3,2)\|UNREACTED CARBON DIOXIDE(3,2)\|ACCESSORY OXIDE(3,1)\|ACTIVE QUARRY(3,1)\|ANTIGORITE REACTION(3,1)\|ASBESTOS BACK DEHYDRATION(3,1)\|BEST MECHANISTIC REACTION(3,1)\|BULK ORE(3,1)\|CARBON ECONOMY PURSUIT(3,1)\|CARBON MINERALIZATION KINETIC RATE(3,1)\|CARBON MINERALIZATION RATE(3,1)\|CARBON NEGATIVE CONCRETE FDLER(3,1)\|CARBON NEUTRAL PURSUIT(3,1)\|CARBON SEQUESTERING CARBONATION REACTION(3,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(3,1)\|CEMENT MANUFACTURING(3,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(3,1)\|CIRCUMNEUTRAL PH(3,1)\|CO2 OCCURRENCE(3,1)\|COMPETING REACTION OCCURRENCE(3,1)\|COMPLEX CHEMISTRY(3,1)\|CONCENTRATE SCARCE METAL(3,1)\|CONTAMINANT GAS(3,1)\|CRUSHED GROUND ORE(3,1)\|DENSER IRON SILICATE(3,1)\|DERIVATIVE UTILIZATION(3,1)\|DESCRIPTIVE SENSE(3,1)\|DEVELOPMENT EFFORT(3,1)\|DISPOSITIONING(3,1)\|ELEVATED IRON CONTENT(3,1)\|ENHANCE KINETICS(3,1)\|ENHANCED MAGNETITE PRODUCTION(3,1)\|EXPERIMENTAL RUN(3,1)\|EXPLOIT GEOLOGICAL FORMATION(3,1)\|EXPLOITATION(3,1)\|EXTRACT HYDROGEN(3,1)\|FAYALITE HYDRATION REACTION(3,1)\|FC SBO(3,1)\|FC SFO(3,1)\|FLUID GEOCHEMISTRY(3,1)\|FLUID SAMPLING PORT(3,1)\|FORSTEIITE COMPONENT(3,1)\|FORSTERITE REACTION(3,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(3,1)\|GENERIC SENSE(3,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(3,1)\|GRAVITY SEPARATOR(3,1)\|GREEN AMMONIA(3,1)\|GREEN GOLDEN HYDROGEN(3,1)\|GROUNDWATER TREATMENT(3,1)\|HYDROGEN GENERATION COPRODUCT(3,1)\|IRON RICH IRON SILICA(3,1)\|IRON RICH MINERAL(3,1)\|IRON RICH OLIVINE(3,1)\|LABILE CARBON(3,1)\|MACHINERY PLACEMENT(3,1)\|MAGNESITE FORMATION(3,1)\|MAGNESITE GENERATION(3,1)\|MAGNESITE VALUE UTILIZATION(3,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(3,1)\|MAGNESIUM RICH SILICATE MINERAL(3,1)\|MAGNESIUM SILICATE CONVERSION(3,1)\|MAGNETITE PARTICLE(3,1)\|MAGNETITE REMOVAL(3,1)\|MAGNETITE YIELD(3,1)\|MEANINGFUL BENEFIT(3,1)\|METHANE CONVERSION(3,1)\|MG SIO(3,1)\|MIL NACL SALINE SOLUTION(3,1)\|MILDLY ACIDIC CONDITION(3,1)\|MILDLY ACIDIC SOLUTION(3,1)\|MINERAL PROCESSING(3,1)\|MINERAL SECONDARY RECOVERY(3,1)\|MINERAL SLAG(3,1)\|MUNICIPAL WASTEWATER TREATMENT(3,1)\|OLIVINE MINERAL PHASE(3,1)\|OLIVINE TEST(3,1)\|PH AMENDMENT(3,1)\|PHASE MINERAL UNITY(3,1)\|PREEVACUATED SAMPLE CHAMBER(3,1)\|PRIMARY DIFFERENTIATOR(3,1)\|PROCESSED ROCK(3,1)\|PYROXENE BEARING LOCALITY(3,1)\|REMAINING ROCK UNREACTED ORE(3,1)\|REMAINING UNREACTED ORE(3,1)\|RESIDUAL IRON SILICATE(3,1)\|RESIDUAL OLIVINE(3,1)\|ROBUST DEPOSIT(3,1)\|ROCK CONTENT(3,1)\|ROCK PREPARATION PHASE(3,1)\|SCARCE METAL RESOURCE(3,1)\|SEALED REACTOR(3,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(3,1)\|SERPENTINIZATION HYDRATION REACTION(3,1)\|SERPENTINIZATION REACTION KINETIC RATE(3,1)\|SERPENTINIZATION REACTION PHASE(3,1)\|SOHD REACTION PRODUCT(3,1)\|SOLUTION GLOBAL APPLICABILITY(3,1)\|SPEX BALL MILL(3,1)\|SR QUADRUPOLE MASS SPECTROMETER(3,1)\|STANDARD GEOTHERMOMETER(3,1)\|STOICHIOMETRIC PROPORTION(3,1)\|STONE AGGREGATE FORMATION(3,1)\|TARGET PRODUCTION(3,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(3,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(3,1)\|ULTRAMAFIC FORMATION(3,1)\|UNDESIRED MINERAL SPECIES(3,1)\|UNIFORM SIZING(3,1)\|VALENCE(3,1)\|VARIABLE OXYGEN FUGACITY(3,1)\|VISIBLE OLIVINE(3,1)\|WATER LOWERED OXYGEN FUGACITY(3,1)\|MAGNESIUM OXIDE(2,4)\|STOICHIOMETRIC RATIO(2,4)\|CARBON DIOXIDE GAS(2,3)\|FACILITY(2,3)\|GRINDER(2,3)\|HYDROGEN GAS EVOLUTION(2,3)\|IRON SILICATE PHASE(2,3)\|MEMBRANE SEPARATION(2,3)\|PRELIMINARY RESULT(2,3)\|SULFUR DIOXIDE(2,3)\|FLOWCHART BLOCK(2,2)\|FOSSIL FUEL COMBUSTION(2,2)\|STEAM METHANE REFORMING(2,2)\|ABIOTIC HYDROGEN PRODUCTION(2,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(2,1)\|ALUMINOSILICATE(2,1)\|AMPLIFICATION(2,1)\|ATMOSPHERIC CONDITION(2,1)\|ATTRACTION(2,1)\|BATCH CONDITION(2,1)\|CARBON DIOXIDE EMISSION(2,1)\|CARBON DIOXIDE PURITY(2,1)\|CARBON DIOXIDE REACTIVITY(2,1)\|CARBON NEGATIVE CONCRETE FILLER(2,1)\|CARBON SEQUESTRATION CAPACITY(2,1)\|CRASHER(2,1)\|DECADE(2,1)\|EXPANSION VOLUME(2,1)\|FINE POWDER(2,1)\|FLUID CHEMISTRY(2,1)\|GEOLOGICAL SOURCE(2,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(2,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(2,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(2,1)\|INCREASED MINERALIZATION(2,1)\|INCREASED REACTIVITY(2,1)\|REACHING RESERVE(2,1)\|\|(JP2024528907)\|REACTOR(100,242)\|ORE(100,85)\|ROCK(100,54)\|MAGNETITE(100,34)\|HYDROGEN PRODUCTION(100,24)\|PRESELECTED SIZE(100,22)\|PYROXENE(100,22)\|INLET(100,21)\|KANLANITE(100,16)\|ORE PARTICLE(100,12)\|CRUSHER(100,9)\|SIEVE(100,9)\|CARBON(100,7)\|ISOLATING CARBON(100,7)\|OUTLET(100,6)\|SUPPLY SOURCE(100,5)\|RECEIVE ONLY ORE PARTICLE(100,1)\|ORE INTRODUCTION(71,4)\|REMAINING ORE(64,38)\|OBTAINING ORE(62,3)\|MAGNETITE ORE(58,44)\|ROUGH STONE(57,3)\|MINERAL AGGREGATE COMPLEX(37,1)\|PRODUCING MAGNETITE ORE(34,2)\|GANGLIOLITE SUBSTANCE(34,1)\|THERMODYNAMIC EQUILIBRIUM(33,2)\|ULTRAMAGNETIC IGNEOUS ROCK(32,2)\|MAGNETITE ATTRACTION(32,1)\|ORE GRINDING(31,2)\|MAGNETIC ORE(31,1)\|CARBON DIOXIDE(30,147)\|SEQUENTIAL CARBONATION REACTION(30,1)\|MINERAL AGGREGATE(29,2)\|SIFTING ORE(29,1)\|ACIDIC SOLUTION(28,11)\|WATER OXYGEN FUGACITY(27,6)\|PRODUCING MAGNESIUM CARBONATE(27,2)\|MAGNESIUM SILICATE CONVERSION(26,1)\|FLUID COMMUNICATION(25,3)\|APPENDIX(24,103)\|REMAINING ROCK(24,5)\|ORE PARTICLE COATING(24,1)\|CARBON DIOXIDE PRESSURE(22,31)\|CARBONATION REACTION(22,15)\|AMBIENT TEMPERATURE(22,9)\|SERPENTINIZATION(22,7)\|SEQUESTERING CARBON(22,1)\|FINE POWDER(21,1)\|SCENARIO(21,1)\|MAGNETIC SEPARATOR(20,7)\|RAW STONE(20,6)\|CARBONATE MINERAL(20,4)\|MAGNESITE(19,31)\|CHROMIUM(19,11)\|ORE TREATMENT(19,1)\|MAGNESIUM CARBONATE(18,41)\|SUPERCRITICAL CARBON DIOXIDE(18,6)\|COBALT(17,13)\|CARBON DIOXIDE MINERALIZATION(17,5)\|PYROXITE(17,2)\|QUANLANITE(17,1)\|REMAINING IRON SILICATE(17,1)\|HYDROGEN GAS(16,55)\|GRINDING(16,6)\|YOUNG MARINE CRUST(16,5)\|GAS SEPARATOR(15,10)\|CRUSHING(15,4)\|REMOVING OXYGEN(15,4)\|PHYLLOITE(15,1)\|CARBON ISOLATION(14,5)\|CAMLANITE(14,3)\|IRON SILICATE(13,21)\|SMALL SIZED PIECE(12,7)\|PYROXENE RICH ORE(12,6)\|ROCK MASS(12,4)\|PARTICLE DIAMETER(12,1)\|HYDRATION REACTION(11,9)\|LITHIUM(11,4)\|BITTERN KANLANITE MINERAL(11,3)\|BITTERN KANLAN MINERAL REACTIVITY(11,1)\|USEFUL COMPONENT REMOVAL(11,1)\|REACTION PRODUCT(10,22)\|INORGANIC PHASE(10,17)\|ATMOSPHERIC PRESSURE(10,11)\|CARBONIZATION REACTION(10,7)\|MAGNESIUM SILICATE(10,3)\|ULTRAFINE IGNEOUS ROCK(10,2)\|BITTEROUS ROCK RESERVE(10,1)\|FERROUS SILICEOUS PYROXENE(10,1)\|IRON KANLANITE MINERAL PRECONCENTRATION(10,1)\|STUBBORN PYROXENE STONE(10,1)\|RESIDENCE TIME(9,53)\|REACTION STEP(9,32)\|ROCK POWDER(9,4)\|CLEANER(9,3)\|FERROUS KANLANITE(9,3)\|MAGNETITE ORE PRODUCTION(9,3)\|SERPENTINE LITHOTRIZATION REACTION(9,2)\|SUPERFINE MAFIC IGNEOUS ROCK(9,1)\|RARE EARTH ELEMENT(8,14)\|DENSITY SEPARATION(8,7)\|UTILITY COMPONENT(8,3)\|IRON SILICEOUS STONE MINERAL(8,2)\|PULVERIZED ROCK(8,2)\|SUPERMAFIC ROCK(8,2)\|ULTRAMAGNETIC ROCK(8,2)\|ULTRAMUTITE ROCK(8,2)\|BITTERN KANRAN STONE MINERAL(8,1)\|HOMOGENIZED KANLANITE MINERAL(8,1)\|IRON SILICENE PYROXENE MINERAL(8,1)\|MAGNESITE RICH ORE(8,1)\|QUARRIED KANLANITE(8,1)\|REACTION RESULT(8,1)\|ROBUST MAFIC DEPOSIT(8,1)\|ROCK AGGREGATE SERPENTINIZATION REACTION(8,1)\|WEATHERED MINERAL EXTRACTION(8,1)\|RARE METAL(7,22)\|IRON SILICATE MINERAL(7,4)\|RETENTION TIME(7,3)\|ROCK MINERAL(7,3)\|SMALL SIZED FRAGMENT(7,3)\|THERMOCOUPLE DETECTOR(7,3)\|UNREACTED ROCK ORE(7,3)\|STONE AGGREGATE(7,2)\|BITTERNESS SUPERBITTEROUS ORE(7,1)\|ULTRAMAGNETIC MAGNOLITE(7,1)\|CARBON NEUTRAL(6,6)\|CENTRAL RIDGE(6,5)\|NONBIOLOGICAL HYDROGEN GENERATION(6,4)\|SMALL PIECE(6,4)\|CHEMICAL PROPERTY(6,2)\|FERROUS SILICATE(6,2)\|FRACTIONAL COEFFICIENT(6,2)\|MAGNETITE MAGNESITE GENERATION(6,2)\|OXYGEN FUGASITY(6,2)\|BIGENTOUS PYROXITE(6,1)\|BIGENTRIC PYROXENE(6,1)\|BITTERN CALCINITE(6,1)\|BITTERN KANOLITE(6,1)\|BITTEROUS ROCK ORE(6,1)\|IRON CAMELANITE MINERAL(6,1)\|IRON KANLAN ROCK(6,1)\|KINETIC LAW STUDY(6,1)\|MAGNETITE ORE GENERATION(6,1)\|NEUTRALIZE ACIDIFICATION(6,1)\|OXYGEN FUGA CITY(6,1)\|PROMOTING SERPENTINIZATION(6,1)\|ROCK PULVERIZATION(6,1)\|SERPENTINIZING REACTION REACTIVITY(6,1)\|SOLID MATERIAL(6,1)\|STUBBLE PYROXENE(6,1)\|STUBBORN CALCINITE(6,1)\|STUBBORN TERMITE(6,1)\|ULTRAFINE METEOROID(6,1)\|ULTRAMERETIC ROCK BULK SAMPLE(6,1)\|UNREACTED IRON KANLANITE(6,1)\|VOLUNTARY PRIVATE SECTOR EFFORT(6,1)\|CARBON NEGATIVE(5,8)\|COPPER FLOOR(5,3)\|PRODUCTION PROMOTION(5,3)\|SRI GAS CHROMATOGRAPH(5,3)\|BAND HEATER(5,2)\|BATCH EXPERIMENT(5,2)\|CERAMIC BRICK(5,2)\|CO2 MINERALIZATION RATE(5,2)\|GASEOUS CO2(5,2)\|GEOLOGICAL SITE(5,2)\|INORGANIC PARTICLE(5,2)\|IRON KANOLITE MINERAL(5,2)\|IRON SILICEOUS MINERAL PHASE(5,2)\|MAGNESITE MINERAL PHASE(5,2)\|MAGNESITE PRODUCTION(5,2)\|RESIDUAL VEIN(5,2)\|ROUGH PUMP(5,2)\|SEPARATING ROCK(5,2)\|ARBITRARY SLAG SUBSTANCE(5,1)\|BITTERN KANRAN MINERAL(5,1)\|BITTERN LANTHANUM MINERAL(5,1)\|CARBON MINERALIZATION EXPERIMENT(5,1)\|CARBONATION REACTION ACCELERATOR(5,1)\|DEHYDRATING ASBESTOS(5,1)\|EARTH CONTINENTAL CRUST(5,1)\|ECONOMIC GEOLOGICAL HYDROGEN(5,1)\|EXPANDABLE MAGNESITE FORMATION(5,1)\|FERROUS CALCINITE REACTION(5,1)\|GANGOLITE MINERAL(5,1)\|IRON SERPENTINIZATION(5,1)\|IRON SILICA PYROXENE(5,1)\|MINERAL CARBONATE(5,1)\|MUNICIPAL SEWAGE(5,1)\|NEUTRALIZING ACIDIFICATION(5,1)\|OBLIQUE TERMITE(5,1)\|PULSATING STONE(5,1)\|REMAINING BULK ROCK GEOCHEMICAL(5,1)\|SILICEOUS ROCK(5,1)\|STEAM METHANE REFORMING REACTION(5,1)\|STOICHIOMETRIC MODELING(5,1)\|STOICHIOMETRIC SERPENTINE REACTION(5,1)\|SUPERBITTERLIKE ROCK(5,1)\|SUPERBITTEROUS ROCK(5,1)\|SUPERMUNITIC ROCK(5,1)\|ULTRAMAGNETIC ORE(5,1)\|ULTRAMATERIOUS ROCK(5,1)\|ULTRAMERETIC ROCK ORE(5,1)\|GRAVITY SEPARATION(4,8)\|HEAVY LIQUID SEPARATION(4,6)\|REACTION CONDITION(4,6)\|FERTILIZER(4,4)\|GRAVEL(4,4)\|DIHYDROGEN SULFIDE(4,3)\|IRON RICH SILICATE MINERAL(4,3)\|LANDFILL(4,3)\|NATURAL REACTION(4,3)\|PHANOLITE(4,3)\|REMAINING ROCK ORE(4,3)\|SEQUENTIAL REACTION(4,3)\|STRATUM(4,3)\|CARBON DIOXIDE SEQUESTRATION(4,2)\|CARBON MINERALIZATION RATE(4,2)\|COMPETITIVE REACTION(4,2)\|OMEGA K WIRE THERMOCOUPLE(4,2)\|RESIDUAL GAS ANALYZER(4,2)\|WEAKLY ACIDIC SOLUTION(4,2)\|AGGREGATE SALE(4,1)\|AMBIENT OXYGEN FUGACITY(4,1)\|ANTIGOLITE REACTION(4,1)\|BITTEROUS ROCK COMPONENT(4,1)\|BULK ORE(4,1)\|CARBON MINERALIZATION KINETIC RATE(4,1)\|CARBONATED MINERAL PHASE(4,1)\|CLEAN ORE(4,1)\|CO2 REACTION(4,1)\|COPPER SCRAP FLOOR(4,1)\|CRUSHED ORE(4,1)\|EXPOSED IRON KANLANITE(4,1)\|EXTRACTING HYDROGEN(4,1)\|FLUID GEOCHEMISTRY(4,1)\|GOVERNMENT IMPOSED REGULATION(4,1)\|GRAVITY SEPARATOR(4,1)\|GROUNDWATER TREATMENT(4,1)\|HARMFUL MINERAL PHASE(4,1)\|HYPOXIA FUGACITY WATER(4,1)\|HYPOXIC FUGACITY WATER(4,1)\|INTRODUCING ROCK(4,1)\|IRON KANLANITE MINERAL PHASE(4,1)\|IRON KANOLANITE(4,1)\|IRON PYROXENE(4,1)\|IRON RICH KANLANITE(4,1)\|IRON SILICANITE(4,1)\|IRON TERMITE(4,1)\|ISOLATION TAX CREDIT(4,1)\|KANLAN STONE TEST SAMPLE(4,1)\|KANLANITE RICH ORE(4,1)\|MAFIC IGNEOUS ROCK SOURCE(4,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(4,1)\|MAGNETITE PARTICLE(4,1)\|MAGNETITE YIELD(4,1)\|MEANINGFUL BENEFIT(4,1)\|MINERAL SLAG(4,1)\|ORE RESIDUE(4,1)\|ORIGIN GENE(4,1)\|OXYGEN FUGATIVITY(4,1)\|PAST FEW DECADE(4,1)\|PURITY CO2(4,1)\|PYROLYSIS REACTION(4,1)\|REACTING CRUSHED GROUND ROCK(4,1)\|REACTIVITY BENEFIT(4,1)\|REMAINING ROCK UNREACTED ORE(4,1)\|REMAINING UNREACTED MINERAL(4,1)\|REMAINING UNREACTED ORE ROCK(4,1)\|ROCK HAMMER(4,1)\|ROCK METRIC TON(4,1)\|ROCK ORE DECOMPOSITION(4,1)\|ROCK PARTICLE(4,1)\|SCIENTIFIC SUPPLIER(4,1)\|SECTION REACTION STEP(4,1)\|SENDING DEVICE REMAINING ORE(4,1)\|SEQUENTIAL CARBON ISOLATION CARBONATION(4,1)\|SEQUENTIAL CARBONIZATION(4,1)\|SEQUENTIAL SERPENTINIZATION REACTION(4,1)\|SOIL KANLANITE(4,1)\|SOLUTION GLOBAL APPLICABILITY(4,1)\|SPEX BALL MILL(4,1)\|STANDARD GEOTHERMAL ANALYZER(4,1)\|STOICHIOMETRIC CALCULATION(4,1)\|STOICHIOMETRIC EVALUATION(4,1)\|SUPER BITTEROUS ROCK(4,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(4,1)\|ULTRAMAFIC DEPOSIT(4,1)\|VISIBLE KANLANITE(4,1)\|WATER OXYGEN FUGAL CITY(4,1)\|GRINDING MACHINE(3,5)\|SODIUM BICARBONATE(3,5)\|POTASSIUM HYDROXIDE(3,4)\|SODIUM HYDROXIDE(3,4)\|PATHWAY(3,3)\|AGRICULTURAL LIME(3,2)\|ATTACHMENT DRAWING(3,2)\|BLUE SITE(3,2)\|CARBON NEGATIVE CONCRETE FILLER(3,2)\|ELECTROLYSIS(3,2)\|GANGUE(3,2)\|MAGNESIUM COMPONENT(3,2)\|MG2SIO(3,2)\|PRESELECTED TEMPERATURE(3,2)\|SINK(3,2)\|SUBSTITUTE(3,2)\|SUPERCRITICAL CO2(3,2)\|TERMIITE(3,2)\|UNREACTED CARBON DIOXIDE(3,2)\|ACCELERATE REMOVAL(3,1)\|ACTIVE QUARRY(3,1)\|AIRTIGHT STAINLESS STEEL(3,1)\|ARBITRARY ACTION(3,1)\|CARBON DIOXIDE SEGREGATION(3,1)\|CARBON INTENSIVE CONSTRAINT(3,1)\|CARBON NEUTRAL PURSUIT(3,1)\|CARBONATION SERPENTINE REACTION PRODUCT(3,1)\|CEMENT PRODUCTION(3,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(3,1)\|CO2 GENERATION(3,1)\|COMPONENT ABUNDANCE(3,1)\|CRUSHED GROUND ORE(3,1)\|DEBATE(3,1)\|DEEP COLD SEPARATION(3,1)\|DENSE IRON SILICATE(3,1)\|DEVELOPMENT EFFORT(3,1)\|EXPLANATORY SENSE(3,1)\|FINE PARTICULATE(3,1)\|FLUID SAMPLING PORT(3,1)\|GAS ALLICOTE(3,1)\|GASEOUS CARBON DIOXIDE ISOLATION(3,1)\|GENERATING MAGNETITE(3,1)\|GENERATING ORE(3,1)\|GEOCHEMICAL CONDITION(3,1)\|GREEN AMMONIA(3,1)\|GREEN GOLDEN HYDROGEN(3,1)\|IMPURITY GAS(3,1)\|IRON KANRAN MINERAL PHASE(3,1)\|IRON ORE RICH(3,1)\|IRON RICH IRON SILICA(3,1)\|IRON RICH MINERAL(3,1)\|ISOLATING HYDROGEN(3,1)\|MAGNESITE VALUE(3,1)\|MAGNESIUM RICH SILICATE MINERAL(3,1)\|MAGNETITE PRODUCTION(3,1)\|MAGNETITE REMOVAL(3,1)\|METHANE CONVERSION(3,1)\|METHANE FORMATION(3,1)\|OBTAINING ROCK(3,1)\|ORE OVER TIME(3,1)\|OXYGEN FUGAL CITY WATER(3,1)\|PASS ORE PARTICLE(3,1)\|PRODUCING MAGNETITE(3,1)\|REMAINING ROCK PULSATE(3,1)\|ROCK CONTENT(3,1)\|ROCK KG(3,1)\|ROCK PREPARATION PHASE(3,1)\|SEALED REACTOR(3,1)\|SEPARATING SIO2(3,1)\|SERPENTINE FORMATION REACTION(3,1)\|SERPENTINIZATION HYDRATION(3,1)\|SR QUADRUPOLE MASS SPECTROMETER(3,1)\|STONE TREATMENT(3,1)\|SUBPHASE COMPETITIVE PHASE(3,1)\|TARGET PRODUCTION(3,1)\|TOTAL CARBON MINERALIZATION(3,1)\|TRACE CO2(3,1)\|ULTRAMUTITE SOURCE(3,1)\|UNEXTRACTABLE MINERAL PHASE LAYER(3,1)\|URBAN SEWAGE TREATMENT(3,1)\|WASTE FLOWING KANLANITE(3,1)\|WATER OXYGEN FUMARICITY(3,1)\|WEAKLY ACIDIC AQUEOUS SOLUTION(3,1)\|WEAKLY ACIDIC CONDITION(3,1)\|STOICHIOMETRIC RATIO(2,5)\|GEOLOGICAL LAYER(2,4)\|CARBON DIOXIDE GAS(2,3)\|FLUIDIZED BED(2,3)\|IRON SILICATE PHASE(2,3)\|PRELIMINARY RESULT(2,3)\|ROTARY KILN(2,3)\|SO2(2,3)\|SULFUR DIOXIDE(2,3)\|CASTING(2,2)\|FLOWCHART BLOCK(2,2)\|FOSSIL FUEL COMBUSTION(2,2)\|ACCESSORY MINERAL PHASE(2,1)\|ACCOUNTING(2,1)\|ALUMINOSILICATE(2,1)\|ATTRACTION(2,1)\|BARGE(2,1)\|BATCH CONDITION(2,1)\|CANLANITE(2,1)\|CARBON DIOXIDE EMISSION(2,1)\|CARBON DIOXIDE INTRODUCTION(2,1)\|CARBON DIOXIDE PURITY(2,1)\|CARBON DIOXIDE REACTIVITY(2,1)\|CARBON SEQUESTRATION CAPACITY(2,1)\|CHANGING PH(2,1)\|CO2 RATIO(2,1)\|CONCENTRATE(2,1)\|DIFFERENTIATOR(2,1)\|DISPOSAL(2,1)\|DIVERSE CHEMICAL PROPERTY FORMATION(2,1)\|FE SILICITE(2,1)\|FE2SI2O(2,1)\|FE2SIO(2,1)\|FLUID CHEMISTRY(2,1)\|GAS PURGE ACTION(2,1)\|GAS REACTION(2,1)\|GASEOUS CARBON DIOXIDE REACTION(2,1)\|GEOLOGICAL SOURCE(2,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(2,1)\|\|(IN202417013808)\|REACTOR(100,174)\|MAGNETITE(100,64)\|ROCK(100,35)\|HYDROGEN(100,25)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,7)\|H DROGEN(100,1)\|ORE(69,64)\|REMAINING ORE(69,31)\|ORE PARTICLE(57,11)\|MAGNESITE SEQUENTIAL CARBONATION(53,1)\|MAFIC IGNEOUS ROCK(45,7)\|ROCK ASSEMBLAGE(43,1)\|ULTRAMAFIC IGNEOUS ROCK(42,7)\|PYROXENE RICH ORE(40,16)\|OLIVINE(36,34)\|COMMINUTING(36,6)\|COPPER FILING HEATED BED(34,4)\|THERMODYNAMIC EQUILIBRIUM(32,2)\|RESIDENCE RIME(32,1)\|PRESELECTED SIZE(31,13)\|ACIDIC SOLUTION(31,7)\|WATER OXYGEN FUGACITY(29,4)\|PYROXENE BEARING ORE(29,3)\|CARBON DIOXIDE(28,112)\|MINERAL ASSEMBLAGE(28,2)\|COMPLEX MINERALOGY(28,1)\|PYROXENE(27,20)\|SERPENTINIZATION REACTION(24,24)\|GAS SEPARATOR(22,11)\|AMBIENT TEMPERATURE(22,6)\|MAGNESIUM CARBONATE(20,39)\|CHROMIUM(19,9)\|MAGNETIC SEPARATOR(19,7)\|SUPERCRITICAL CARBON DIOXIDE(19,3)\|SCARCE METAL PRODUCTION(18,1)\|HYDROGEN GAS(17,50)\|COBALT(17,11)\|CARBON INTENSIVE(17,2)\|SCARCE METAL(16,16)\|CARBON DIOXIDE MINERALIZATION(16,5)\|PRODUCING MAGNETITE(16,4)\|HYDROGEN FORMATION(16,1)\|NATURAL GAS REFORMING(16,1)\|MAGNESITE(15,29)\|CRUSHER(14,5)\|FLUID COMMUNICATION(14,3)\|NATURAL GAS AVAILABILITY(14,1)\|VAIYING REACTION CONDITION(14,1)\|RESIDENCE TIME(12,37)\|SIEVE(12,9)\|ROCK POWDER(11,6)\|LITHIUM(11,3)\|CHEMISTRY(11,2)\|ATMOSPHERIC PRESSURE(10,8)\|PATHWAY(10,7)\|COMMINUTED ROCK(10,4)\|FORSTERITE MINERAL(10,4)\|IMMENSE GEOLOGICAL SCALABILITY(10,1)\|REACTION PRODUCT(9,22)\|INORGANIC PHASE(9,17)\|PRECIOUS METAL(9,7)\|OLIVINE RICH ORE(9,2)\|DESIRED MINERAL(9,1)\|RARE EARTH ELEMENT(8,12)\|CARBON SEQUESTRATION(8,9)\|CARBONIZATION REACTION(8,5)\|UNREACTED ROCK ORE(8,3)\|GANGUE MATERIAL(8,2)\|WEATHERED MINERAL MINING(8,1)\|YOUNG OCEANIC CMST(8,1)\|CRUSHED GROUND ROCK(7,6)\|WASHER(7,3)\|ECONOMIC VIABILITY(7,2)\|NEUTRALIZE ACIDIFICATION(7,2)\|FAYALITE PRECONCENTRATION(7,1)\|FAYALITE SERPENTINIZATION(7,1)\|MAFIC IGNEOUS ROCK POTENTIAL(7,1)\|MAFIC ULTRAMAFIC ORE(7,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(7,1)\|MINERAL GRAIN COMMINUTION(7,1)\|OLIVINE RICH DEPOSIT(7,1)\|SUPERCRITICAL CAIBON DIOXIDE(7,1)\|ACCESSORY MINERAL COLLECTION(6,3)\|THERMOCOUPLE DETECTOR(6,3)\|AGGREGATE SUBSTITUTE(6,2)\|FERROSILITE MINERAL PHASE(6,2)\|MAFIC IGNEOUS ROCK SOURCE(6,2)\|PULVERIZED ROCK(6,2)\|RESIDUAL GANGUE(6,2)\|UNREACTED ORE ROCK(6,2)\|CARBON MINERALIZATION KINETICS(6,1)\|GASEOUS CO2 DISSOLUTION(6,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(6,1)\|OLIVINE ABUNDANCE(6,1)\|ORE CARBONATION DRIVEN COMMINUTION(6,1)\|PYROXENE MINERALOGY(6,1)\|RELEVANT CONSTITUENT ABUNDANCE(6,1)\|REVENUE ENTITLEMENT(6,1)\|SEQUESTRATION TAX CREDIT(6,1)\|SERPENTINIZATION REACTION REACTIVITY(6,1)\|SERPENTINIZED ULTRAMAFIC ROCK(6,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(6,1)\|SMALL SIZE FRACTION(5,10)\|CARBON NEUTRAL(5,6)\|SRI GAS CHROMATOGRAPH(5,3)\|BAND HEATER(5,2)\|BATCH EXPERIMENT(5,2)\|CERAMIC BRICK(5,2)\|FRACTIONATION FACTOR(5,2)\|GEOLOGICAL SITE(5,2)\|MAGNETITE MAGNESITE PRODUCTION(5,2)\|PYROLYSIS REACTION(5,2)\|RELEVANT COMPONENT(5,2)\|REMAINING ROCK GANGUE(5,2)\|ROUGH PUMP(5,2)\|ABIOGENIC METHANE FORMATION(5,1)\|CARBON MINERALIZATION EXPERIMENT(5,1)\|COMMINUTED ORE(5,1)\|EARTH CONTINENTAL CRUST(5,1)\|ECONOMIC GEOLOGICAL HYDROGEN(5,1)\|FORSTERITE AVAILABILITY(5,1)\|GANGUE MINERAL(5,1)\|GASEOUS CAIBON REACTION(5,1)\|HOMOGENIZED OLIVINE(5,1)\|HYDROGEN EVOLUTION KINETICS(5,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(5,1)\|NONCONDENSABLE FRACTION(5,1)\|REMAINING BULK ROCK GEOCHEMICAL(5,1)\|ROCK ORE BREAKDOWN(5,1)\|SCALABLE MAGNESITE(5,1)\|SCIENTIFIC SUPPLIER(5,1)\|SEQUENTIAL CARBONIZATION(5,1)\|STEAM METHANE REFORMING REACTION(5,1)\|STOICHIOMETRIC ASSESSMENT(5,1)\|STOICHIOMETRIC MODELING(5,1)\|UNREACTED FAYALITE(5,1)\|YOUNG OCEANIC CRUST(5,1)\|REACTOR VESSEL(4,9)\|GRAVITY SEPARATION(4,8)\|FERTILIZER(4,4)\|PRESELECTED TEMPERATURE(4,4)\|STANDARD OMEGA(4,4)\|ACCOUNTING(4,3)\|DIHYDROGEN SULFIDE(4,3)\|ELECTRICITY(4,3)\|EVEN CARBON NEGATIVE(4,3)\|IRON RICH SILICATE MINERAL(4,3)\|LANDFILL(4,3)\|NATURAL REACTION(4,3)\|REMAINING ROCK ORE(4,3)\|ROTARY KILN(4,3)\|SEQUENTIAL REACTION(4,3)\|VALUABLE CONSTITUENT(4,3)\|COMPETITION(4,2)\|COPPER BED(4,2)\|OLIVINE WASTE STREAM(4,2)\|OMEGA K WIRE THERMOCOUPLE(4,2)\|RESIDUAL GAS ANALYZER(4,2)\|AGGREGATE SALE(4,1)\|AMBIENT OXYGEN FUGACITY(4,1)\|CARBONATE MINERALIZATION(4,1)\|COMMENSURATE LY(4,1)\|ENABLED EXPERIMENTATION(4,1)\|ENSTATITE MINERAL(4,1)\|GOVERNMENT MANDATED REGULATION(4,1)\|MAGNETITE RECOVERY(4,1)\|MID OCEANIC RIDGE(4,1)\|MINERAL BREAKDOWN(4,1)\|MITIGATE ATMOSPHERIC RELEASE(4,1)\|PROLIFIC OCCURRENCE(4,1)\|QUARRYING CONCEPT(4,1)\|REACTION SEQUENTIAL ORDERING(4,1)\|ROCK HAMMER(4,1)\|ROCK METRIC TON(4,1)\|SEQUENTIAL SERPENTINIZATION REACTION(4,1)\|STEAM REFORMER(4,1)\|STOICHIOMETRIC CALCULATION(4,1)\|THERMOCHEMICAL DRIVER(4,1)\|ULTRAMAFIC ROCK BULK SAMPLE(4,1)\|REACTION STEP(3,25)\|HEAVY LIQUID SEPARATION(3,5)\|SODIUM BICARBONATE(3,5)\|POTASSIUM HYDROXIDE(3,4)\|PSI PRESSURE GAUGE(3,4)\|ACCESSORY MINERAL PHASE(3,2)\|AGRICULTURAL LIME(3,2)\|BRUCITE(3,2)\|CARBON DIOXIDE INTRODUCTION(3,2)\|CRUSHING(3,2)\|ELECTROLYSIS(3,2)\|ENHANCING PRODUCTION(3,2)\|MAGNESIUM COMPONENT(3,2)\|MAGNETITE REACTION PRODUCT(3,2)\|METAL ENRICHMENT(3,2)\|SOURCE ROCK COMMINUTION(3,2)\|ULTRAMAFIC AGGREGATE MATERIAL(3,2)\|UNREACTED CARBON DIOXIDE(3,2)\|ACCESSORY OXIDE(3,1)\|ACTIVE QUARRY(3,1)\|ANTIGORITE REACTION(3,1)\|ASBESTOS BACK DEHYDRATION(3,1)\|BEST MECHANISTIC REACTION(3,1)\|BULK ORE(3,1)\|CARBON ECONOMY PURSUIT(3,1)\|CARBON MINERALIZATION KINETIC RATE(3,1)\|CARBON MINERALIZATION RATE(3,1)\|CARBON NEGATIVE CONCRETE FDLER(3,1)\|CARBON NEUTRAL PURSUIT(3,1)\|CARBON SEQUESTERING CARBONATION REACTION(3,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(3,1)\|CEMENT MANUFACTURING(3,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(3,1)\|CO2 OCCURRENCE(3,1)\|COMPETING REACTION OCCURRENCE(3,1)\|COMPLEX CHEMISTRY(3,1)\|CONCENTRATE SCARCE METAL(3,1)\|CONTAMINANT GAS(3,1)\|CRUSHED GROUND ORE(3,1)\|CRYOGENIC SEPARATION(3,1)\|DENSER IRON SILICATE(3,1)\|DERIVATIVE UTILIZATION(3,1)\|DESCRIPTIVE SENSE(3,1)\|DEVELOPMENT EFFORT(3,1)\|DISPOSITIONING(3,1)\|ELEVATED IRON CONTENT(3,1)\|ENHANCE KINETICS(3,1)\|ENHANCED MAGNETITE PRODUCTION(3,1)\|EXPERIMENTAL RUN(3,1)\|EXPLOIT GEOLOGICAL FORMATION(3,1)\|EXPLOITATION(3,1)\|EXTRACT HYDROGEN(3,1)\|FAYALITE HYDRATION REACTION(3,1)\|FC SBO(3,1)\|FC SFO(3,1)\|FLUID GEOCHEMISTRY(3,1)\|FLUID SAMPLING PORT(3,1)\|FORSTEIITE COMPONENT(3,1)\|FORSTERITE REACTION(3,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(3,1)\|GENERIC SENSE(3,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(3,1)\|GRAVITY SEPARATOR(3,1)\|GREEN AMMONIA(3,1)\|GREEN GOLDEN HYDROGEN(3,1)\|GROUNDWATER TREATMENT(3,1)\|HYDROGEN GENERATION COPRODUCT(3,1)\|IRON RICH IRON SILICA(3,1)\|IRON RICH MINERAL(3,1)\|IRON RICH OLIVINE(3,1)\|LABILE CARBON(3,1)\|MACHINERY PLACEMENT(3,1)\|MAGNESITE FORMATION(3,1)\|MAGNESITE GENERATION(3,1)\|MAGNESITE VALUE UTILIZATION(3,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(3,1)\|MAGNESIUM RICH SILICATE MINERAL(3,1)\|MAGNESIUM SILICATE CONVERSION(3,1)\|MAGNETITE PARTICLE(3,1)\|MAGNETITE REMOVAL(3,1)\|MAGNETITE YIELD(3,1)\|MEANINGFUL BENEFIT(3,1)\|METHANE CONVERSION(3,1)\|MG SIO(3,1)\|MIL NACL SALINE SOLUTION(3,1)\|MILDLY ACIDIC CONDITION(3,1)\|MILDLY ACIDIC SOLUTION(3,1)\|MINERAL PROCESSING(3,1)\|MINERAL SECONDARY RECOVERY(3,1)\|MINERAL SLAG(3,1)\|MUNICIPAL WASTEWATER TREATMENT(3,1)\|OLIVINE MINERAL PHASE(3,1)\|OLIVINE TEST(3,1)\|PHASE MINERAL UNITY(3,1)\|PREEVACUATED SAMPLE CHAMBER(3,1)\|PRIMARY DIFFERENTIATOR(3,1)\|PROCESSED ROCK(3,1)\|PYROXENE BEARING LOCALITY(3,1)\|REMAINING ROCK UNREACTED ORE(3,1)\|REMAINING UNREACTED ORE(3,1)\|RESIDUAL IRON SILICATE(3,1)\|RESIDUAL OLIVINE(3,1)\|ROBUST DEPOSIT(3,1)\|ROCK CONTENT(3,1)\|ROCK PREPARATION PHASE(3,1)\|SCARCE METAL RESOURCE(3,1)\|SEALED REACTOR(3,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(3,1)\|SERPENTINIZATION HYDRATION REACTION(3,1)\|SERPENTINIZATION REACTION KINETIC RATE(3,1)\|SERPENTINIZATION REACTION PHASE(3,1)\|SIO2 DENSITY SEPARATION(3,1)\|SOHD REACTION PRODUCT(3,1)\|SOLUTION GLOBAL APPLICABILITY(3,1)\|SPEX BALL MILL(3,1)\|SR QUADRUPOLE MASS SPECTROMETER(3,1)\|STANDARD GEOTHERMOMETER(3,1)\|STOICHIOMETRIC PROPORTION(3,1)\|STONE AGGREGATE FORMATION(3,1)\|TARGET PRODUCTION(3,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(3,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(3,1)\|ULTRAMAFIC FORMATION(3,1)\|UNDESIRED MINERAL SPECIES(3,1)\|UNIFORM SIZING(3,1)\|VARIABLE OXYGEN FUGACITY(3,1)\|VISIBLE OLIVINE(3,1)\|WATER LOWERED OXYGEN FUGACITY(3,1)\|MAGNESIUM OXIDE(2,4)\|STOICHIOMETRIC RATIO(2,4)\|CARBON DIOXIDE GAS(2,3)\|FACILITY(2,3)\|FLUIDIZED BED(2,3)\|GRINDER(2,3)\|HYDROGEN GAS EVOLUTION(2,3)\|IRON SILICATE PHASE(2,3)\|PRELIMINARY RESULT(2,3)\|SULFUR DIOXIDE(2,3)\|FLOWCHART BLOCK(2,2)\|FOSSIL FUEL COMBUSTION(2,2)\|ABIOTIC HYDROGEN PRODUCTION(2,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(2,1)\|ALUMINOSILICATE(2,1)\|AMPLIFICATION(2,1)\|ATMOSPHERIC CONDITION(2,1)\|ATTRACTION(2,1)\|CARBON DIOXIDE EMISSION(2,1)\|CARBON DIOXIDE PURITY(2,1)\|CARBON DIOXIDE REACTIVITY(2,1)\|CARBON NEGATIVE CONCRETE FILLER(2,1)\|CARBON SEQUESTRATION CAPACITY(2,1)\|CRASHER(2,1)\|DECADE(2,1)\|ENHANCING CARBON DIOXIDE(2,1)\|EXPANSION VOLUME(2,1)\|FINE POWDER(2,1)\|FLUID CHEMISTRY(2,1)\|GEOLOGICAL SOURCE(2,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(2,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(2,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(2,1)\|INCREASED MINERALIZATION(2,1)\|INCREASED REACTIVITY(2,1)\|INORGANIC PRODUCT(2,1)\|INTENDED CARBONATION REACTION(2,1)\|REACHING RESERVE(2,1)\|\|(AU2022318480)\|REACTOR(100,174)\|MAGNETITE(100,64)\|ROCK(100,34)\|HYDROGEN(100,26)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,7)\|ORE(69,64)\|REMAINING ORE(69,31)\|ORE PARTICLE(57,11)\|MAGNESITE SEQUENTIAL CARBONATION(53,1)\|MAFIC IGNEOUS ROCK(45,7)\|ROCK ASSEMBLAGE(43,1)\|ULTRAMAFIC IGNEOUS ROCK(42,7)\|PYROXENE RICH ORE(41,16)\|OLIVINE(36,34)\|COMMINUTING(36,6)\|COPPER FILING HEATED BED(34,4)\|THERMODYNAMIC EQUILIBRIUM(32,2)\|PRESELECTED SIZE(31,13)\|ACIDIC SOLUTION(31,7)\|WATER OXYGEN FUGACITY(29,4)\|CARBON DIOXIDE(28,114)\|PYROXENE BEARING ORE(28,3)\|MINERAL ASSEMBLAGE(28,2)\|COMPLEX MINERALOGY(28,1)\|PYROXENE(27,20)\|SERPENTINIZATION REACTION(24,24)\|GAS SEPARATOR(22,11)\|AMBIENT TEMPERATURE(22,6)\|MAGNESIUM CARBONATE(20,39)\|CHROMIUM(19,9)\|MAGNETIC SEPARATOR(19,7)\|SUPERCRITICAL CARBON DIOXIDE(18,4)\|SCARCE METAL PRODUCTION(18,1)\|HYDROGEN GAS(17,50)\|COBALT(17,11)\|CARBON INTENSIVE(17,2)\|SCARCE METAL(16,16)\|CARBON DIOXIDE MINERALIZATION(16,5)\|PRODUCING MAGNETITE(16,4)\|HYDROGEN FORMATION(16,1)\|NATURAL GAS REFORMING(16,1)\|MAGNESITE(15,29)\|CRUSHER(14,6)\|FLUID COMMUNICATION(14,3)\|NATURAL GAS AVAILABILITY(14,1)\|OLIVINE PYROXENE SERPENTINE FORSTERITE(14,1)\|RESIDENCE TIME(12,38)\|SIEVE(12,9)\|ROCK POWDER(11,6)\|LITHIUM(11,3)\|CHEMISTRY(11,2)\|ATMOSPHERIC PRESSURE(10,8)\|PATHWAY(10,7)\|COMMINUTED ROCK(10,4)\|FORSTERITE MINERAL(10,4)\|IMMENSE GEOLOGICAL SCALABILITY(10,1)\|MAFIC ROCK REACHING RESERVE(10,1)\|REACTION PRODUCT(9,22)\|INORGANIC PHASE(9,17)\|PRECIOUS METAL(9,7)\|OLIVINE RICH ORE(9,2)\|DESIRED MINERAL(9,1)\|RARE EARTH ELEMENT(8,12)\|CARBON SEQUESTRATION(8,9)\|CARBONIZATION REACTION(8,5)\|UNREACTED ROCK ORE(8,3)\|GANGUE MATERIAL(8,2)\|WEATHERED MINERAL MINING(8,1)\|CRUSHED GROUND ROCK(7,6)\|WASHER(7,3)\|ECONOMIC VIABILITY(7,2)\|NEUTRALIZE ACIDIFICATION(7,2)\|YOUNG OCEANIC CRUST(7,2)\|FAYALITE PRECONCENTRATION(7,1)\|FAYALITE SERPENTINIZATION(7,1)\|MAFIC IGNEOUS ROCK POTENTIAL(7,1)\|MAFIC ULTRAMAFIC ORE(7,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(7,1)\|MINERAL GRAIN COMMINUTION(7,1)\|OLIVINE RICH DEPOSIT(7,1)\|ACCESSORY MINERAL COLLECTION(6,3)\|THERMOCOUPLE DETECTOR(6,3)\|AGGREGATE SUBSTITUTE(6,2)\|FERROSILITE MINERAL PHASE(6,2)\|MAFIC IGNEOUS ROCK SOURCE(6,2)\|PULVERIZED ROCK(6,2)\|RESIDUAL GANGUE(6,2)\|UNREACTED ORE ROCK(6,2)\|CARBON MINERALIZATION KINETICS(6,1)\|GASEOUS CO2 DISSOLUTION(6,1)\|IGNEOUS MINERAL CO2(6,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(6,1)\|OLIVINE ABUNDANCE(6,1)\|ORE CARBONATION DRIVEN COMMINUTION(6,1)\|PYROXENE MINERALOGY(6,1)\|RELEVANT CONSTITUENT ABUNDANCE(6,1)\|REVENUE ENTITLEMENT(6,1)\|SEQUESTRATION TAX CREDIT(6,1)\|SERPENTINIZATION REACTION REACTIVITY(6,1)\|SERPENTINIZED ULTRAMAFIC ROCK(6,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(6,1)\|SMALL SIZE FRACTION(5,10)\|CARBON NEUTRAL(5,6)\|COPPER BED(5,3)\|SRI GAS CHROMATOGRAPH(5,3)\|BAND HEATER(5,2)\|BATCH EXPERIMENT(5,2)\|CERAMIC BRICK(5,2)\|CO2 MINERALIZATION RATE(5,2)\|FRACTIONATION FACTOR(5,2)\|GEOLOGICAL SITE(5,2)\|MAGNETITE MAGNESITE PRODUCTION(5,2)\|PYROLYSIS REACTION(5,2)\|RELEVANT COMPONENT(5,2)\|ROUGH PUMP(5,2)\|ABIOGENIC METHANE FORMATION(5,1)\|CARBON MINERALIZATION EXPERIMENT(5,1)\|COMMINUTED ORE(5,1)\|EARTH CONTINENTAL CRUST(5,1)\|ECONOMIC GEOLOGICAL HYDROGEN(5,1)\|FORSTERITE AVAILABILITY(5,1)\|GANGUE MINERAL(5,1)\|HOMOGENIZED OLIVINE(5,1)\|HYDROGEN EVOLUTION KINETICS(5,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(5,1)\|NONCONDENSABLE FRACTION(5,1)\|REMAINING BULK ROCK GEOCHEMICAL(5,1)\|ROCK ORE BREAKDOWN(5,1)\|SCALABLE MAGNESITE(5,1)\|SCIENTIFIC SUPPLIER(5,1)\|SEQUENTIAL CARBONIZATION(5,1)\|STEAM METHANE REFORMING REACTION(5,1)\|STOICHIOMETRIC ASSESSMENT(5,1)\|STOICHIOMETRIC MODELING(5,1)\|ULTMMAFIC ROCK(5,1)\|UNREACTED FAYALITE(5,1)\|REACTOR VESSEL(4,9)\|GRAVITY SEPARATION(4,8)\|REACTION CONDITION(4,6)\|CRUSHING(4,4)\|FERTILIZER(4,4)\|PRESELECTED TEMPERATURE(4,4)\|STANDARD OMEGA(4,4)\|ACCOUNTING(4,3)\|DIHYDROGEN SULFIDE(4,3)\|ELECTRICITY(4,3)\|EVEN CARBON NEGATIVE(4,3)\|IRON RICH SILICATE MINERAL(4,3)\|LANDFILL(4,3)\|NATURAL REACTION(4,3)\|REMAINING ROCK ORE(4,3)\|SEQUENTIAL REACTION(4,3)\|VALUABLE CONSTITUENT(4,3)\|COMPETITION(4,2)\|OLIVINE WASTE STREAM(4,2)\|OMEGA K WIRE THERMOCOUPLE(4,2)\|REMAINING ROCK GANGUE(4,2)\|RESIDUAL GAS ANALYZER(4,2)\|SUPERCRITICAL CO2(4,2)\|AGGREGATE SALE(4,1)\|AMBIENT OXYGEN FUGACITY(4,1)\|CARBONATE MINERALIZATION(4,1)\|ENABLED EXPERIMENTATION(4,1)\|ENSTATITE MINERAL(4,1)\|GOVERNMENT MANDATED REGULATION(4,1)\|MAGNETITE RECOVERY(4,1)\|MID OCEANIC RIDGE(4,1)\|MINERAL BREAKDOWN(4,1)\|MITIGATE ATMOSPHERIC RELEASE(4,1)\|PROLIFIC OCCURRENCE(4,1)\|QUARRYING CONCEPT(4,1)\|REACTION SEQUENTIAL ORDERING(4,1)\|ROCK HAMMER(4,1)\|ROCK METRIC TON(4,1)\|SEQUENTIAL SERPENTINIZATION REACTION(4,1)\|STEAM REFORMER(4,1)\|STOICHIOMETRIC CALCULATION(4,1)\|THERMOCHEMICAL DRIVER(4,1)\|ULTRAMAFIC ROCK BULK SAMPLE(4,1)\|REACTION STEP(3,24)\|HEAVY LIQUID SEPARATION(3,5)\|MGCO3(3,5)\|SODIUM BICARBONATE(3,5)\|POTASSIUM HYDROXIDE(3,4)\|PSI PRESSURE GAUGE(3,4)\|ACCESSORY MINERAL PHASE(3,2)\|AGRICULTURAL LIME(3,2)\|BRUCITE(3,2)\|CARBON DIOXIDE INTRODUCTION(3,2)\|CARBON NEGATIVE CONCRETE FILLER(3,2)\|ELECTROLYSIS(3,2)\|ENHANCING PRODUCTION(3,2)\|FE2SIO(3,2)\|MAGNESIUM COMPONENT(3,2)\|MAGNETITE REACTION PRODUCT(3,2)\|METAL ENRICHMENT(3,2)\|MG2SIO(3,2)\|SOURCE ROCK COMMINUTION(3,2)\|ULTRAMAFIC AGGREGATE MATERIAL(3,2)\|UNREACTED CARBON DIOXIDE(3,2)\|ACCESSORY OXIDE(3,1)\|ACTIVE QUARRY(3,1)\|ANTIGORITE REACTION(3,1)\|ASBESTOS BACK DEHYDRATION(3,1)\|BEST MECHANISTIC REACTION(3,1)\|BULK ORE(3,1)\|CARBON ECONOMY PURSUIT(3,1)\|CARBON MINERALIZATION KINETIC RATE(3,1)\|CARBON MINERALIZATION RATE(3,1)\|CARBON NEUTRAL PURSUIT(3,1)\|CARBON SEQUESTERING CARBONATION REACTION(3,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(3,1)\|CEMENT MANUFACTURING(3,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(3,1)\|CIRCUMNEUTRAL PH(3,1)\|CO2 OCCURRENCE(3,1)\|CO2 REDUCTION(3,1)\|COMPETING REACTION OCCURRENCE(3,1)\|COMPLEX CHEMISTRY(3,1)\|CONCENTRATE SCARCE METAL(3,1)\|CONTAMINANT GAS(3,1)\|CRUSHED GROUND ORE(3,1)\|CRYOGENIC SEPARATION(3,1)\|DENSER IRON SILICATE(3,1)\|DERIVATIVE UTILIZATION(3,1)\|DESCRIPTIVE SENSE(3,1)\|DEVELOPMENT EFFORT(3,1)\|DISPOSITIONING(3,1)\|ELEVATED IRON CONTENT(3,1)\|ENHANCE KINETICS(3,1)\|ENHANCED MAGNETITE PRODUCTION(3,1)\|EXPERIMENTAL RUN(3,1)\|EXPLOIT GEOLOGICAL FORMATION(3,1)\|EXPLOITATION(3,1)\|EXTRACT HYDROGEN(3,1)\|FAYALITE HYDRATION REACTION(3,1)\|FLUID GEOCHEMISTRY(3,1)\|FLUID SAMPLING PORT(3,1)\|FORSTERITE COMPONENT(3,1)\|FORSTERITE REACTION(3,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(3,1)\|GENERIC SENSE(3,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(3,1)\|GRAVITY SEPARATOR(3,1)\|GREEN AMMONIA(3,1)\|GREEN GOLDEN HYDROGEN(3,1)\|GROUNDWATER TREATMENT(3,1)\|HYDROGEN GENERATION COPRODUCT(3,1)\|IRON RICH IRON SILICA(3,1)\|IRON RICH MINERAL(3,1)\|IRON RICH OLIVINE(3,1)\|LABILE CARBON(3,1)\|MACHINERY PLACEMENT(3,1)\|MAGNESITE FORMATION(3,1)\|MAGNESITE GENERATION(3,1)\|MAGNESITE VALUE UTILIZATION(3,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(3,1)\|MAGNESIUM RICH SILICATE MINERAL(3,1)\|MAGNESIUM SILICATE CONVERSION(3,1)\|MAGNETITE PARTICLE(3,1)\|MAGNETITE REMOVAL(3,1)\|MAGNETITE YIELD(3,1)\|MEANINGFUL BENEFIT(3,1)\|METHANE CONVERSION(3,1)\|MIL NACL SALINE SOLUTION(3,1)\|MILDLY ACIDIC CONDITION(3,1)\|MILDLY ACIDIC SOLUTION(3,1)\|MINERAL PROCESSING(3,1)\|MINERAL SECONDARY RECOVERY(3,1)\|MINERAL SLAG(3,1)\|MUNICIPAL WASTEWATER TREATMENT(3,1)\|OLIVINE MINERAL PHASE(3,1)\|OLIVINE TEST(3,1)\|PH AMENDMENT(3,1)\|PHASE DECARBONATION REACTION MOLE(3,1)\|PHASE MINERAL UNITY(3,1)\|PREEVACUATED SAMPLE CHAMBER(3,1)\|PRIMARY DIFFERENTIATOR(3,1)\|PROCESSED ROCK(3,1)\|PURITY CO2(3,1)\|PYROXENE BEARING LOCALITY(3,1)\|REMAINING ROCK UNREACTED ORE(3,1)\|REMAINING UNREACTED ORE(3,1)\|RESIDUAL IRON SILICATE(3,1)\|RESIDUAL OLIVINE(3,1)\|ROBUST DEPOSIT(3,1)\|ROCK CONTENT(3,1)\|ROCK PREPARATION PHASE(3,1)\|SCARCE METAL RESOURCE(3,1)\|SEALED REACTOR(3,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(3,1)\|SERPENTINIZATION REACTION KINETIC RATE(3,1)\|SERPENTINIZATION REACTION PHASE(3,1)\|SIO2 DENSITY SEPARATION(3,1)\|SOLUTION GLOBAL APPLICABILITY(3,1)\|SPEX BALL MILL(3,1)\|SR QUADRUPOLE MASS SPECTROMETER(3,1)\|STANDARD GEOTHERMOMETER(3,1)\|STOICHIOMETRIC PROPORTION(3,1)\|STONE AGGREGATE FORMATION(3,1)\|TARGET PRODUCTION(3,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(3,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(3,1)\|ULTRAMAFIC FORMATION(3,1)\|UNDESIRED MINERAL SPECIES(3,1)\|UNIFORM SIZING(3,1)\|VARIABLE OXYGEN FUGACITY(3,1)\|VISIBLE OLIVINE(3,1)\|WATER LOWERED OXYGEN FUGACITY(3,1)\|MAGNESIUM OXIDE(2,4)\|STOICHIOMETRIC RATIO(2,4)\|CARBON DIOXIDE GAS(2,3)\|FACILITY(2,3)\|FLUIDIZED BED(2,3)\|GRINDER(2,3)\|HYDROGEN GAS EVOLUTION(2,3)\|IRON SILICATE PHASE(2,3)\|PRELIMINARY RESULT(2,3)\|ROTARY KILN(2,3)\|SO2(2,3)\|SULFUR DIOXIDE(2,3)\|FLOWCHART BLOCK(2,2)\|FOSSIL FUEL COMBUSTION(2,2)\|STAINLESS STEEL REACTION VESSEL(2,2)\|ABIOTIC HYDROGEN PRODUCTION(2,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(2,1)\|ALUMINOSILICATE(2,1)\|AMPLIFICATION(2,1)\|ATMOSPHERIC CONDITION(2,1)\|ATTRACTION(2,1)\|BATCH CONDITION(2,1)\|CARBON DIOXIDE EMISSION(2,1)\|CARBON DIOXIDE PURITY(2,1)\|CARBON DIOXIDE REACTIVITY(2,1)\|CARBON SEQUESTRATION CAPACITY(2,1)\|CO2 ELEVATED PRESSURE(2,1)\|CO2 RATIO(2,1)\|DECADE(2,1)\|ENHANCING CARBON DIOXIDE(2,1)\|EXPANSION VOLUME(2,1)\|FINE POWDER(2,1)\|FLUID CHEMISTRY(2,1)\|GEOLOGICAL SOURCE(2,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(2,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(2,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(2,1)\|INCREASED MINERALIZATION(2,1)\|INCREASED REACTIVITY(2,1)\|INORGANIC PRODUCT(2,1)\|INTENDED CARBONATION REACTION(2,1)\|IRON ORE NATURE(2,1)\|\|(CA3227505)\|REACTOR(100,130)\|MAGNETITE(100,60)\|ROCK(100,32)\|HYDROGEN(100,26)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,7)\|HYDROGEN GENERATION(100,6)\|YAWING MINERAL ASSEMBLAGE(84,1)\|ORE(80,48)\|YAWING MINERAL ASSEMBLAGE COMPLEX(76,1)\|REMAINING ORE(67,20)\|ROCK ASSEMBLAGE(62,1)\|NAMIC EQUILIBRIUM(55,1)\|PYROXENE RICH ORE(50,15)\|OLIVINE(49,33)\|MAFIC IGNEOUS ROCK(48,6)\|PYROXENE BEARING ORE(47,2)\|ULTRAMAFIC IGNEOUS ROCK(45,6)\|ORE PARTICLE(43,5)\|COMMINUTING(42,3)\|PYROXENE(40,20)\|COMPLEX MINERALOGY(40,1)\|SERPENTINIZATION REACTION(34,22)\|GAS SEPARATOR(32,11)\|AMBIENT TEMPERATURE(32,6)\|SCARCE METAL PRODUCTION(27,1)\|COPPER FILING HEATED BED(26,2)\|CARBON DIOXIDE(25,92)\|MAGNESIUM CARBONATE(25,37)\|HYDROGEN GAS(24,49)\|CARBON INTENSIVE(24,2)\|CARBON DIOXIDE MINERALIZATION(23,5)\|PRODUCING MAGNETITE(23,4)\|HYDROGEN FORMATION(23,1)\|NATURAL GAS REFORMING(23,1)\|MAGNESITE(22,28)\|WATER OXYGEN FUGACITY(22,2)\|PRESELECTED SIZE(21,5)\|FLUID COMMUNICATION(21,3)\|NATURAL GAS AVAILABILITY(21,1)\|OLIVINE PYROXENE SERPENTINE FORSTERITE(21,1)\|SCARCE METAL(19,15)\|SUPERCRITICAL CARBON DIOXIDE(18,3)\|ROCK POWDER(17,6)\|CHEMISTRY(16,2)\|ATMOSPHERIC PRESSURE(15,8)\|FORSTERITE MINERAL(15,4)\|INORGANIC PHASE(14,17)\|PATHWAY(14,7)\|COMMINUTED ROCK(14,4)\|SEQUENTIAL CARBONATION(14,4)\|OLIVINE RICH ORE(14,2)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|REACTION PRODUCT(13,22)\|DESIRED MINERAL(13,1)\|RESIDENCE TIME(12,22)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|WEATHERED MINERAL MINING(12,1)\|CRUSHED GROUND ROCK(11,6)\|UNREACTED ROCK ORE(11,3)\|LITHIUM(11,2)\|NEUTRALIZE ACIDIFICATION(11,2)\|YOUNG OCEANIC CRUST(11,2)\|FAYALITE PRECONCENTRATION(11,1)\|FAYALITE SERPENTINIZATION(11,1)\|COBALT(10,7)\|CHROMIUM(10,5)\|MAGNETIC SEPARATOR(10,5)\|ECONOMIC VIABILITY(10,2)\|MAFIC IGNEOUS ROCK POTENTIAL(10,1)\|MAFIC ULTRAMAFIC ORE(10,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(10,1)\|MINERAL GRAIN COMMINUTION(10,1)\|OLIVINE RICH DEPOSIT(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|CARBON MINERALIZATION KINETICS(9,1)\|GASEOUS CO2 DISSOLUTION(9,1)\|IGNEOUS MINERAL CO2(9,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(9,1)\|OLIVINE ABUNDANCE(9,1)\|ORE CARBONATION DRIVEN COMMINUTION(9,1)\|PYROXENE MINERALOGY(9,1)\|RELEVANT CONSTITUENT ABUNDANCE(9,1)\|REVENUE ENTITLEMENT(9,1)\|SEQUESTRATION TAX CREDIT(9,1)\|SERPENTINIZATION REACTION REACTIVITY(9,1)\|SERPENTITHZED ULTRAMAFIC ROCK(9,1)\|STOICHIOMCTRIC ASSESSMENT(9,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(9,1)\|SIEVE(8,7)\|CARBON NEUTRAL(8,6)\|BAND HEATER(8,2)\|BATCH EXPERIMENT(8,2)\|CERAMIC BRICK(8,2)\|CO2 MINERALIZATION RATE(8,2)\|FRACTIONATION FACTOR(8,2)\|GEOLOGICAL SITE(8,2)\|MAGNETITE MAGNESITE PRODUCTION(8,2)\|RELEVANT COMPONENT(8,2)\|ROUGH PUMP(8,2)\|UNREACTED ORE ROCK(8,2)\|COPPER BED(7,3)\|RESIDUAL GAS ANALYZER(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|SUPERCRITICAL CO2(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|GREEN TECLMOLOGY(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|NONCONDENSABLE FRACTION(7,1)\|PY ROLYSIS REACTION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STEAM METHANE REFORMING REACTION(7,1)\|STOICHIOMETRIC MODELING(7,1)\|STOICLIIOMETRIC CALCULATION(7,1)\|THERMODYNAMIC EQUILIBRIUM(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|REACTION CONDITION(6,6)\|CRUSHER(6,4)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|DECARBONATION REACTION MOLE(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|IRON OXIDELMAGNETITE(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL ASSEMBLAGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACHING RESERVE(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|RARE EARTH ELEMENT(5,8)\|SMALL SIZE FRACTION(5,7)\|MGCO3(5,6)\|PRECIOUS METAL(5,6)\|HEAVY LIQUID SEPARATION(5,5)\|SODIUM BICARBONATE(5,5)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|MG2SIO(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CIRCUMNCUTRAL PH(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|CRYOGENIC SEPARATION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ELEVATED IMN CONTENT(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GEOLOGICAL HYDROGEN(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH CNDMCMBCR(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROLYSIS REACTION(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SEMENTINIZATION REACTION(5,1)\|SERPCNTINIZATION REACTION(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|THC ROCK(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|TROXENE BEARING ORE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,24)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|ENHANCING PRODUCTION(4,2)\|FE2SIO(4,2)\|FLOWCHART BLOCK(4,2)\|FOSSIL FUEL COMBUSTION(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|STAINLESS STEEL REACTION VESSEL(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|GREEN GOLDEN HYDROGEN(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|BMCITE(3,1)\|BRUCITE(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|DECADE(3,1)\|ENHANCING CARBON DIOXIDE(3,1)\|EXPANSION VOLUME(3,1)\|FE2SI2O(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|INTENDED CARBONATION REACTION(3,1)\|	(US12545576)\|What is claimed is:\|1. A system for sequestering carbon and producing hydrogen and magnetite from rock, the system comprising:\| a source of ore containing olivine or pyroxene;\| a reactor having an inlet that receives ore particles and at least one outlet, the reactor also having at least one additional inlet through which one or more of carbon dioxide or water is introduced, the reactor operable at a first temperature for a first residence time to react carbon dioxide that enters the reactor through the at least one additional inlet with the ore particles to generate magnesium carbonate, the reactor also operable at a second temperature for a second residence time to react water that enters the reactor through the at least one additional inlet with the ore particles to generate magnetite and hydrogen gas; and\| a gas separator that is connected to and in fluid communication with the at least one outlet of the reactor, the gas separator configured to separate hydrogen gas from gases that exit the reactor through the at least one outlet.\|2. The system of claim 1, further comprising a crusher that physically reduces a particle size of the ore introduced therein from the source.\|3. The system of claim 2, further comprising:\| a sieve that receives the ore from the crusher and that allows the ore particles up to a pre-selected size to pass into the reactor,\| wherein the inlet that receives the ore particles is configurable to only receive, from the sieve, the ore particles having a size at or below to the pre-selected size.\|4. The system of claim 3, wherein the pre-selected size comprises a size of between about 25 microns and about 150 microns.\|5. The system of claim 1, wherein a pressure inside the reactor during the second residence time is at or above about 1 bar of carbon dioxide.\|6. The system of claim 5, wherein a pressure inside the reactor during the second residence time is at or above 5 bars of carbon dioxide.\|7. The system of claim 6, wherein a pressure inside the reactor during the second residence time is at or above 10 bars of carbon dioxide.\|8. The system of claim 1, further comprising a magnetic separator that receives material from the at least one outlet of the reactor, the magnetic separator having a magnet that attracts the magnetite and thereby separates the magnetite from the material.\|9. The system of claim 1, further comprising a washer that applies either additional water or an acidic solution to the ore particles prior to their reaction with the carbon dioxide.\|10. The system of claim 1, further comprising a separator that separates at least one of nickel, cobalt, chromium, or rare earth elements from any remaining ore particles removed from the reactor.\|11. The system of claim 1, wherein the reactor includes a first reactor into which the carbon dioxide is introduced and a second reactor into which the water is introduced, the first reactor being operable at the first temperature for the first residence time to react the carbon dioxide that enters the first reactor through the at least one additional inlet with the ore particles, and the second reactor being operable at the second temperature for the second residence time to react the water that enters the second reactor with any remaining ore particles introduced into the second reactor from the first reactor.\|12. The system of claim 1, wherein the water has a pH of between about 8.3 and about 11.1.\|13. The system of claim 1, wherein at least one of the first temperature and the second temperature is no greater than 400° C.\|14. The system of claim 1, wherein at least one of the first temperature and the second temperature is no greater than 300° C.\|15. The system of claim 1, wherein a pressure inside the reactor during the first residence time is at or above about 5 bars of carbon dioxide.\|16. The system of claim 1, wherein the carbon dioxide that is introduced into the reactor is gaseous or supercritical carbon dioxide.\|17. The system of claim 1, further comprising a separator that separates at least one of phosphates, aluminum oxides, precious metals, and other mineral gangue from any remaining ore particles removed from the reactor.\|18. A method for generating hydrogen and magnetite from rock, the method comprising:\| obtaining an ore containing olivine or pyroxene;\| introducing the ore into a reactor that is operable at temperatures above ambient temperature and pressures above atmospheric pressure;\| introducing water into the reactor at a particular temperature for a particular residence time to react with the ore to generate magnetite and hydrogen gas;\| removing, from the reactor, a gas mixture that includes the hydrogen gas;\| separating the hydrogen gas from the gas mixture; and\| removing any remaining ore from the reactor.\|19. The method of claim 18, further comprising washing the ore with either additional water or an acidic solution prior to comminuting the ore into the smaller size fractions.\|20. The method of claim 18, further comprising:\| sieving the ore prior to introducing the ore into the reactor to allow ore particles up to a pre-selected size to pass into the reactor,\| wherein introducing the ore into the reactor comprises introducing, into the reactor, only a subset of the ore having particles up to the pre-selected size.	(US12545576)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This application is a continuation of U.S. application Ser. No. 18/302,702 filed Apr. 18, 2023, which is a continuation of U.S. patent application Ser. No. 17/815,914 filed Jul. 28, 2022, which claims the benefit of U.S. Provisional Patent Application No. 63/203,814 filed Jul. 30, 2021. The entire contents of all of the above applications are incorporated herein by reference.\|(US12545576)\|FIELD OF THE DISCLOSURE\|[0002] One or more embodiments of this disclosure generally relate to systems and methods that produce hydrogen, generate magnetite, and/or derive additional desired products from ores containing olivine or pyroxene (such as mafic and/or ultramafic rocks) through pre-selected chemical processes. In one or more embodiments, the systems and methods facilitate carbonization and/or serpentinization/hydration reactions involving olivine- and pyroxene-rich ores in order to sequester carbon dioxide, liberate hydrogen, generate magnetite and magnesite, and/or derive other desired products, including scarce metals, which are in many cases critical to various green technologies (e.g., batteries, energy storage, photovoltaics) otherwise mined using carbon-intensive methods.\|BACKGROUND\|[0003] The environmental impact of greenhouse gases, primarily carbon dioxide (CO2) and methane (CH4), has been the subject of much public debate over the past several decades. More recently, self-imposed private-sector initiatives and government-mandated regulations to reduce the release of greenhouse gases into the environment have begun to be implemented. In addition to the capture and/or sequestration of carbon dioxide and other greenhouse gases to mitigate their atmospheric release, much research and development effort has been focused on the utilization of alternatives to fossil fuel combustion for energy production in order to reduce the amount of carbon dioxide generated and/or that must be captured and sequestered.\|[0004] Hydrogen (H2) gas holds promise as an energy source (e.g., as hydrogen fuel or through the use of green ammonia) and chemical feedstock (e.g., methanol, ammonia, hydrocarbon fuels) that provides little-to-no greenhouse gas emission upon combustion. Indeed, the combustion of hydrogen gas yields just water as a reaction product. However, hydrogen gas has traditionally been produced using fossil fuels (e.g., via natural gas/methane conversion in a steam reformer), which yields the greenhouse gas carbon dioxide as a reaction product. For example, in the steam-methane reforming reaction mentioned, methane is reacted with steam (i.e., water) to produce hydrogen gas and carbon monoxide. In a subsequent water-gas shift reaction, the carbon monoxide is further reacted with steam to produce carbon dioxide and additional hydrogen gas. The hydrogen gas is subsequently separated from the carbon dioxide through pressure swing adsorption, membrane separation, or another gas separation process. Thus, most hydrogen that is produced in refinery operations, for example, produces greenhouse gases, which must be captured and sequestered to yield meaningful benefit.\|[0005] Alternatively, hydrogen gas may be generated by the electrolysis of water into hydrogen gas and oxygen. The hydrogen gas is subsequently separated from oxygen through pressure swing adsorption, membrane separation, or another gas separation process. Hydrogen production via electrolysis, or partial pyrolysis reactions, requires a substantial amount of electricity. While at least some of the required electricity for hydrogen production via electrolysis and/or partial pyrolysis reactions may be obtained from renewable sources (e.g., wind, solar, and hydroelectric), in practice the majority of the electricity used for this purpose has traditionally been, and continues to be, produced through the combustion of fossils fuels, which also produces greenhouse gases.\|[0006] The abiotic production of hydrogen gas is known to occur in certain geological formations, e.g., at young oceanic crust near a mid-oceanic ridge, as depicted in FIGS. 1A-1D. These natural reactions occur across a range of environmental conditions that include variable pH, oxygen fugacity, chemical composition, and pressure. Such reactions produce variable and complex mineralogy and chemistry but do not predictably produce any specific combination of reaction products. In fact, as generally illustrated in the cross-section photograph of FIG. 2, rock deposits 200 that may yield abiotic hydrogen often contain complex mixtures or layers of difficult-to-extract mineral phases, or will not produce a desired product if other competing reactions are preferred based on in situ geochemical conditions (e.g., variable redox potential (Eh), pH, pore water composition, gas chemical composition, and temperature). For example, hydrogen production is highly variable in nature and its occurrence greatly depends on pH, Eh, and other aspects of fluid geochemistry in pore spaces and at mineral surfaces. Thus, the complex kinetics of reaction phases and the occurrence of competing reactions in natural conditions (e.g., circumneutral pH, variable oxygen fugacity, and variable pore water chemistry) govern the products yielded by these naturally occurring reactions. Certain geological formations and/or the rocks thereof are also known to contain minerals that are conducive to reaction with carbon dioxide under certain conditions to form carbonated mineral phases, e.g., carbonates.\|BRIEF SUMMARY\|[0007] FIG. 3 provides a map that highlights the example locations of selected suitable and/or robust deposits of mafic and ultramafic rock around the world. Olivine- and pyroxene-bearing ores may be found in such mafic and/or ultramafic formations. As can be understood from FIG. 3, sources of mafic and ultramafic igneous rocks may be found in many locations and are quite plentiful, accounting for at least 10% of the continental crust of the Earth, which illustrates the global applicability of solutions described herein. More recently, such sources of mafic and ultramafic igneous rock have garnered interest for their potential exploitation to sequester (mineralize) carbon dioxide in carbonate mineral phases. However, despite significant prior work on carbon sequestration, there is considerable debate about the best mechanistic reactions and optimized rates for carbon mineralization. As such, the economic viability of these processes has not been fully developed, nor has the hydrogen generation and carbon sequestration capacity of mafic and ultramafic rocks been realized. Moreover, no economic use has been identified for the fine-grained carbonated mineral phases that result from carbonization reactions. Rather, proposals have recommended such carbonated mineral phases be used as fill or dumped in oceans or lakes).\|[0008] Despite the theoretical potential for such geological formations and/or the ores thereof to be exploited for geological hydrogen or other products, and for potential carbon sequestration, the processes and kinetics of these reactions has not been rigorously evaluated nor optimized. Further, processes for the production of hydrogen from these geological formations without the occurrence of alternative, and sometimes deleterious, mineral phases (e.g., serpentine, such as antigorite, asbestos) have not been developed. Accordingly, Applicant has recognized a need for systems and methods that exploit certain geological formations and/or the ores thereof to liberate hydrogen, generate magnetite and magnesite, and/or derive other desired products, such as scarce/critical metals from geological formations that include olivine- and pyroxene-rich ores, and in addition, sequester carbon dioxide in magnesite or other mineral phases.\|[0009] The disclosure herein provides one or more embodiments of systems and methods for sequestering carbon, evolving hydrogen gas, and producing magnetite as well as magnesite from olivine- and pyroxene-bearing ores. In addition, precious or scarce metals, such as nickel, cobalt, chromium, and rare earth elements, may be concentrated in the remaining ore, which facilitates their recovery.\|[0010] In an example embodiment, a method is provided for sequestering carbon and producing hydrogen and magnetite. The method includes obtaining an ore that containing olivine or pyroxene. The ore may be comminuted into smaller size fractions, such as by crushing or grinding. The comminuted ore may be introduced into a reactor that is operable at temperatures above ambient temperature and pressures above atmospheric pressure. The method may also include introducing carbon dioxide (or a mixture of carbon dioxide and other gases such as nitrogen (N2), dihydrogen sulfide (H2S), and sulfur dioxide (SO2) into the reactor at a first temperature above ambient temperature for a first residence time to react at least a portion of the carbon dioxide with the ore. The method also includes later introducing water into the reactor at a second temperature for a second residence time to react at least a portion of the water with one or more of the remaining ore to generate at least magnetite and hydrogen gas. Reaction products, including hydrogen gas, magnesium carbonate (magnesite), magnetite, other reaction products, and any remaining ore may be removed from the reactor.\|[0011] In another embodiment, a method is provided for sequestering carbon and generating hydrogen and magnetite from rock. The method includes obtaining an ore that olivine or pyroxene. As above, the ore may be broken down into smaller size fractions, such as by crushing or grinding. The ore is introduced into a first reactor that is operable at a first temperature above ambient temperature and pressures above atmospheric pressure. The method also includes introducing carbon dioxide (or a mixture of carbon dioxide and other gases such as nitrogen (N2), dihydrogen sulfide (H2S), and sulfur dioxide (SO2)) into the first reactor at the first temperature for a first residence time to react at least a portion of the carbon dioxide with the ore to generate at least magnesium carbonate. The remaining ore may be passed to a second reactor. Reaction products from the first reactor may be separated from the remaining ore or may also be passed to the second reactor. The method also includes introducing water into the second reactor at a second temperature for a second residence time to react at least a portion of the water with the remaining ore in the second reactor to produce at least magnetite and hydrogen gas. Reaction products, including hydrogen gas, magnesium carbonate (magnesite), magnetite, other reaction products and any remaining ore may be removed from the second reactor.\|[0012] In yet another embodiment, a system is provided for sequestering carbon and producing hydrogen and magnetite from rock. The system includes a source of ore that contains olivine or pyroxene. The system may include a crusher or grinder used to physically reduce the particle size of the ore introduced therein from the source. The system may include a sieve used to receive the ore from the crusher and configured to allow ore particles up to a pre-selected size to pass therethrough. The system also includes a reactor having an inlet that receives ore particles up to the pre-selected size from the sieve and at least one outlet. The reactor also has at least one additional inlet through which one or more of carbon dioxide or water may be introduced (and in some embodiments, the reactor may comprise two reactors: a first reactor having an additional inlet through which carbon dioxide may be introduced, and a second reactor having another additional inlet through which water may be introduced). The reactor is operable at a first temperature for a first residence time to react at least a portion of any received carbon dioxide with the ore in the first reactor to generate at least magnesium carbonate. The reactor is also operable at a second temperature for a second residence time to react at least a portion of any water that enters the reactor through the at least one additional inlet with any ore within the reactor to generate magnetite and hydrogen gas. In one or more embodiments, the system also includes a gas separator that is connected to and in fluid communication with the at least one outlet of the reactor. The gas separator is configured to separate hydrogen gas from gases that exit the reactor through at least one outlet of the reactor.\|[0013] Corresponding means for performing these various steps are set forth below.\|[0014] The foregoing brief summary is provided merely for purposes of summarizing some example embodiments described herein. Because the above-described embodiments are merely examples, they should not be construed to narrow the scope of this disclosure in any way. It will be appreciated that the scope of the present disclosure encompasses many potential embodiments in addition to those summarized above, some of which will be described in further detail below.\|(US12545576)\|BRIEF DESCRIPTION OF THE FIGURES\|[0015] Having described certain example embodiments in general terms above, reference will now be made to the accompanying drawings, which are not necessarily drawn to scale. Some embodiments may include fewer or more components than those shown in the figures.\|[0016] FIGS. 1A, 1B, 1C, and 1D illustrate cross-sectional representations of young oceanic crust and associated structures positioned near a theoretical mid-oceanic ridge that may produce and/or host abiotic hydrogen production.\|[0017] FIG. 2 illustrates an example cross-section of serpentinized ultramafic rock.\|[0018] FIG. 3 illustrates a map with locations of suitable olivine- and pyroxene-bearing localities throughout the world.\|[0019] FIG. 4A provides an example flow diagram illustrating a sequence of operations performed by a system to enhance carbon dioxide sequestration, hydrogen gas evolution, and magnetite and magnesite production using a single reactor, in accordance with some example embodiments described herein.\|[0020] FIG. 4B provides an example flow diagram illustrating a sequence of operations performed by a system to enhance carbon dioxide sequestration, hydrogen gas evolution, and magnetite/magnesite production using multiple reactors, in accordance with some example embodiments described herein.\|[0021] FIG. 5 illustrates an example flowchart for enhancing carbon dioxide sequestration, hydrogen gas evolution, and magnetite/magnesite production, in accordance with some example embodiments described herein.\|[0022] FIG. 6 illustrates an example flowchart for acquisition and preparation of source rock for reaction, in accordance with some example embodiments described herein.\|[0023] FIG. 7 illustrates an example flowchart for processing rock remaining following any carbon dioxide and/or water reactions, in accordance with some example embodiments described herein.\|(US12545576)\|DETAILED DESCRIPTION\|[0024] Some example embodiments will now be described more fully hereinafter with reference to the accompanying figures, in which some, but not necessarily all, embodiments are shown. Because inventions described herein may be embodied in many different forms, the invention should not be limited solely to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will satisfy applicable legal requirements.\|Overview\|[0025] Applicant recognized that despite the significant theoretical potential of mafic and/or ultramafic igneous rocks (or, more broadly, olivine- and pyroxene-bearing ores, such as those with elevated iron content), as described above, to serve as geological sources for economic geological hydrogen, to be exploited as natural sources and catalysts for hydrogen and magnetite production, and to be exploited for carbon sequestration, the optimal processes and kinetics for these reactions have not been rigorously evaluated nor optimized. Specifically, process steps to enhance both carbon sequestration and the production of hydrogen, magnetite, magnesite, and/or other minerals from these types of rocks—without the formation of alternative (and sometimes deleterious, e.g., serpentine, asbestos) mineral phases—have not been developed.\|[0026] Further, Applicant is unaware of any prior attempts to use an optimized chemical process of carbon mineralization to enhance the kinetics of hydrogen and magnetite production, or to regulate the chemical species of the resulting reaction products (e.g., prevent the formation of serpentine and asbestos).\|[0027] In various embodiments disclosed herein, carbon dioxide may be sequestered, and hydrogen, magnetite, and other scarce metals may be produced economically (and with a neutral to net-negative carbon footprint) using olivine- and pyroxene-rich ores through sequential carbonation and serpentinization reactions in a controlled environment. Thus, Applicant has developed an engineering process that employs sequential reactions to exploit the potential for olivine- and pyroxene-rich ores to both sequester carbon dioxide dominantly as magnesite or other carbonate minerals, as well as liberate hydrogen, magnetite, and/or other desirable minerals/scarce metals. Applicant further recognized that additional process steps applied to the olivine- and pyroxene-rich ores may enhance the concentration and recovery of precious or scarce metals (e.g., nickel, cobalt, chromium, lithium, and rare earth elements.), which are needed for renewable energy and energy storage, among other uses.\|[0028] Applicant discovered that the serpentinization reaction process can be advantaged such that the chemical activity and commensurate rates of reactions between water and fayalite and/or ferrosilite may be enhanced by first removing a significant component of forsterite from the olivine mineral phase and increasing the comminution of mineral grains by inducing the described chemical reactions. In this way, the fayalite and/or ferrosilite in the igneous rock is concentrated and/or becomes less obscured by adjacent minerals, e.g., forsterite. This process benefits the reaction in two ways: first, by enhancing the surface area of fayalite and/or ferrosilite exposed for the reaction; and second, by pre-concentrating the reactant (iron-rich olivine (fayalite) or pyroxene (ferrosilite)) of choice. Thus, in one or more embodiments, forsterite and/or enstatite are at least partially removed prior to reacting the fayalite and/or ferrosilite with water.\|[0029] Some primary differentiators that demonstrate the value of example ex situ engineered embodiments that produce hydrogen, magnesite, magnetite, and critical metals via this pathway include: 1) the immense geological scalability of such embodiments once the “serpentinization” processes are optimized to produce the desired products (hydrogen, magnetite, scarce metals), as opposed to alternative mineral phases such as serpentine, asbestos, etc.; 2) the potential to permanently and verifiably sequester CO2 in a mineralized form and hence produce hydrogen, magnetite, and scarce metals in a carbon-negative process; and 3) the price point of potentially scalable “green” or “golden” hydrogen (i.e., carbon negative hydrogen), magnetite, and scarce metals, which can be greatly offset by considering other values streams generated using the quarrying concept (i.e., the sale of aggregate or higher value utilization of magnesite).\|[0030] Although a high-level explanation of the operations of example embodiments has been provided above, specific details regarding the configuration of such example embodiments are provided below.\|Serpentinization and Carbonation Reactions\|[0031] The disclosure herein provides one or more embodiments of systems and methods that facilitate the production of hydrogen, magnetite, and/or other desired minerals through serpentinization reactions involving olivine- and pyroxene-rich ores generally found in mafic and/or ultramafic igneous rock, or of any other rock assemblages containing such olivine- and pyroxene-rich ores. Table 1, provided below, gives representative serpentinization reactions involving fayalite (Fe2SiO4) and/or ferrosilite (Fe2Si2O6). Fayalite is a mineral phase that is the iron-rich endmember of the olivine solid solution series and is abundant in olivine-rich orc. Ferrosilite is the iron-rich endmember of the orthopyroxene solid solution series and is associated with pyroxene-rich ore. Fayalite and ferrosilite are commonly found together in mafic and ultramafic igneous rocks. Under certain conditions, water reacts with fayalite and ferrosilite to generate magnetite (Fe3O4), silica (SiO2), and hydrogen gas (H2) in the appropriate stoichiometric ratios. In each case, two moles of hydrogen gas are produced from three moles of either fayalite or ferrosilite mineral.\|[0032] TABLE 1 Hydrogen-Generating Serpentinization ReactionsSerpentinization Reactions Moles of MineralSerpentinizationIgneousMolesMineralPhaseReactionMineralof H2 OlivineFayalite3 Fe2 + 2 H2O →32 2 Fe3O4 + 3 SiO2 + 2 H2 PyroxeneFerrosilite3 Fe2Si2O6 + 2 H2O →32 2 Fe3O4 + 6 SiO2 + 2 H2 \|[0033] In one or more embodiments, the disclosed systems and methods may also facilitate the sequestration of gaseous carbon dioxide as mineralized carbonates through carbonation reactions involving the magnesium-rich endmember of olivine- and pyroxene-rich ores found typically in mafic and/or ultramafic rock. Table 2, provided below, gives representative carbonation reactions involving forsterite (Mg2SiO4) and enstatite (Mg2Si2O6), as well as illustrating the potential for carbonation during reaction with antigorite (Mg3Si2O5(OH)4) that can be formed as an accessory mineral phase in natural systems in which fluid conditions are not idealized for the formation of magnesite. Forsterite is a mineral phase that is the magnesium-rich endmember of the olivine solid solution series associated with olivine-rich ore. Enstatite is a mineral phase that is the magnesium-rich endmember of the orthopyroxene solid solution series associated with pyroxene-rich ore. Antigorite is an example mineral phase that is associated with serpentine. Under certain conditions, carbon dioxide reacts with forsterite and enstatite, and/or other accessory mineral phases (e.g., antigorite) to generate at least magnesium carbonate (MgCO3) and silica (SiO2) in appropriate stoichiometric ratios. The reaction of antigorite with carbon dioxide further yields a stoichiometric quantity of water and is shown to illustrate serpentinization reactions that occur in natural systems in which pH, Eh, temperature, pressure, and fluid chemistry cannot be optimized. In the case of the idealized carbonization reaction involving forsterite and enstatite, two moles of carbon dioxide gas are converted to magnesium carbonate (magnesite) per mole of either forsterite or enstatite mineral.\|[0034] TABLE 2 Carbon-Sequestering Carbonation ReactionsDecarbonation Reactions Moles of MineralDecarbonationIgneousMolesMineralPhaseReactionMineralof CO2 OlivineForsteriteMg2SiO4 + 2 CO2 →12 2 MgCO3 + SiO2 PyroxeneEnstatiteMg2Si2O6 + 2 CO2 →12 2 MgCO3 + 2 SiO2 SerpentineAntigoriteMg3Si2O5(OH)4 +13 3 CO2 → 3 MgCO3 + 2 SiO2 + 2 H2O \|[0035] In nature, and as previously described, the above-described serpentinization and carbonization reactions occur, but only as a subset of a variety of reactions occurring across a range of environmental conditions in the subsurface or at surface conditions of the earth. As a result, the environmental conditions are often variable and reactions kinetics and pathways are far from ideal. Accordingly, natural reactions are based on the variable (and often dynamic, i.e., changing with time) pH, oxygen fugacity, temperature, pore water chemical composition, gas chemical composition, and pressure found in nature, specifically in the subsurface. The multitude of reactions and potential pathways for those reactions occurring in nature lead to the formation of variable and complex chemistry and assemblages of minerals, but do not predictably produce any specific combination of usable reaction products. Instead, natural systems, which evolve through time and under varying reaction conditions produce complex (and often heterogeneous) complexes of varying mineral assemblages and products of reactions that did not follow the idealized reactions described above, or are slower to reach thermodynamic equilibrium.\|[0036] With respect to olivine and pyroxene mineralogy and chemistry, olivine is a solid solution series (X2SiO4, where X═Mg2+ or Fe2+) between a magnesium silicate (forsterite) and an iron silicate (fayalite) and pyroxene (i.e., orthopyroxene) is a solid solution series (X2Si2O6, where X═Mg2+ or Fe2+) between a magnesium silicate (enstatite) and an iron silicate (ferrosilite). In the olivine-rich deposits of interest, fayalite and ferrosilite are usually the minor constituent and typically range in concentration from 6% to 20%, with the lower range concentrations appearing more commonly in nature. Consequently, the thermochemical activities of fayalite and ferrosilite are relatively low compared to those of the forsterite or enstatite, respectively. Thus, if the olivine or pyroxene obtained from a quarry is crushed and reacted with water at favorable reaction conditions (i.e., controlled for temperatures, pressures, Eh, pH, and fluid composition, then a serpentinization reaction will proceed at a relatively low rate due to relatively low thermochemical activity and commensurately low rates of reactions with fayalite or ferrosilite. Nevertheless, when completed, the reaction produces magnetite, silica, and hydrogen (from the reaction of fayalite or ferrosilite with water) may be separated (magnetically or gravimetrically) from forsterite, enstatite, or magnesite. The mixture of olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite) minerals, however, constitutes an almost an “ideal” mixture that is exceedingly rare in natural systems. However, in an ideal mixture, the chemical activity varies linearly with the mole fraction and is roughly equal to the mole fraction. Thus, the chemical activity and reaction rate can be enhanced by pre-concentrating the abundance of olivine and pyroxene from the bulk ore and specifically the abundance of the iron-rich endmembers of both the olivine and pyroxene solid solution series.\|Ex Situ Sequestration of Carbon Dioxide and Generation of Hydrogen\|[0037] In various embodiments contemplated herein, carbon dioxide may be mineralized, and hydrogen, magnesite, magnetite, and critical metals may be produced economically (and with an overall neutral to net-negative carbon footprint) by an engineered system that causes sequential reactions in the manner shown in the flow diagrams illustrated in FIGS. 4A, 4B, and described in connection with the flowcharts provided in FIGS. 5, 6, and 7.\|[0038] FIG. 4A illustrates a flow diagram of one embodiment 400′ of a system for enhancing the production of hydrogen gas and magnetite from rock that contains a mixture of olivine (e.g., fayalite and forsterite) and pyroxene (e.g., ferrosilite and enstatite) minerals. A source of olivine- and/or pyroxene-rich ores 402 may be fed or introduced into a crusher or grinder 406 that reduces the size of the received ore into smaller size fractions. In one or more embodiments, a washer 404 may optionally be used to wash the ore with water or a mildly acidic solution to remove any contaminants therefrom and prepare the ore for carbonation reactions. The crushed or ground rock is then introduced into a sieve 408 or other such separator that segregates the rock into pre-selected particle ranges. In one or more embodiments, the sieves or grates thereof are sized to pass 150-, 80-, and even 45-micron grains, although different sizing can be utilized. In at least one embodiment, the comminuted rock is a powder or has a powder-like particle size range. Rock that does not pass through the sieve may be returned to the crusher or grinder 406 via a recycle loop 410 to be reduced further in size. The subset of the rock having particles within a pre-selected particle range of the sieve 408, e.g., 150-micron, 80-micron, 45-micron, or any size therebetween, is then fed or introduced into a reactor 412.\|[0039] The reactor 412 may be a rotary kiln, a toroidal fluidized bed, a fluidized bed, or another reactor known to those skilled in the art. The reactor 412 may have an inlet that receives ore (or ore particles) at least one outlet, from which any remaining ore may be removed following reaction within the reactor 412. The reactor 412 may further have at least one additional inlet through which one or more of carbon dioxide or water can be introduced into the reactor 412. The reactor 412 may be operable at a first temperature for a first residence time to react carbon dioxide that enters the reactor 412 through the at least one additional inlet with ore disposed within the reactor 412 to generate magnesium carbonate. The reactor 412 may further be operable at a second temperature for a second residence time to react water that enters the reactor through the at least one additional inlet (which may be the same inlet by which carbon dioxide enters the reactor 412 or a different inlet) with ore disposed within the reactor 412 to generate magnetite and hydrogen gas.\|[0040] In a first reaction step, carbon dioxide is introduced into reactor 412 with the crushed/ground rock. Water (approximately 10 liters of water per kilogram) may be applied (sprayed or washed) to the crushed/ground rock by washer 404 either before or after placement of the rock into the reactor 412. The wetting of the powdered rock with water allows for the dissolution of gaseous CO2 to carbonic acid (H2CO3) on the wet surfaces of the mineral grains, which enhances the reactivity of the carbon dioxide with the forsterite mineral found therein. In at least one embodiment, the pH of the water applied to the comminuted rock may be between about 4.8 to about 6.5. Water in this pre-selected pH range further enhances the reaction between the carbon dioxide and the forsterite mineral. During this first reaction step, the reactor is operated at a pre-selected temperature (>90° C.) and pressure (greater than approximately five bars) to facilitate the carbonation reaction with respect to the forsterite mineral found in the rock. In one or more embodiments, the reactor 412 is operated at a temperature of between about 100° C. to about 400° C. and at a pressure of between about five and up to at least 100 bars (e.g., about 40, 50, 75 or even 100 bars); note the upper limit of pressure can be extended to considerably higher pressures if the reactor 412 and associated components are able to withstand such pressures. Increasing pressure in this fashion will produce a corresponding enhancement of the carbonation reaction being prompted at this stage of the process. In other embodiments, the operating pressure of the reactor 412 may be as low as 35 bars, as low as 30 bars, as low as 25 bars, as low as 20 bars, as low as 15 bars, as low as 10 bars, as low as 5 bars, or even lower (˜1 bar), and may still prompt the intended carbonation reactions, albeit at commensurately lower rates of reaction. As provided in Table 2 above, the reaction of carbon dioxide with the forsterite (Mg2SiO4) produces magnesium carbonate (MgCO3) and silicon dioxide (SiO2) as reaction products. In this way, the forsterite mineral of the mafic and/or ultramafic rock is used to permanently sequester CO2 in the form of an insoluble magnesium carbonate mineral lattice, which is a solid that that can be useful as a raw material, placed in a landfill, ocean, lake, or otherwise easily stored. By reacting the crushed/ground rock containing the forsterite with carbon dioxide at favorable conditions of temperature, pressure, Eh, and pH, the forsterite can be altered to magnesite following reaction with carbon dioxide.\|[0041] It will be understood that, although this first reaction step favorably enhances the comminution of source rock and better prepares any remaining rock for the second reaction step described below, some embodiments may not perform this first reaction step, and instead may simply comminute the source rock, which itself prepares the source rock for the second reaction step, as illustrated by way of example in the Example Implementation section below. Of course, in other embodiments, the source rock may not need to undergo an initial comminution step, but may instead simply be initially processed using the first reaction step described herein, which itself fosters comminution of the source rock and thus prepares it for more effective reaction in the second reaction step described below. Both comminution of the source rock and the carbonation reactions occurring during the first reaction step favorably dispose any remaining rock for the section reaction step below; accordingly, various combination of comminution and the first reaction step may be employed in various scenarios based on the desired results of a given implementation.\|[0042] In a second reaction step, water is thereafter introduced into reactor 412 with the crushed/ground rock, which may in some embodiments still contain the magnesium carbonate and silicon dioxide from the first reaction step, the fayalite and/or ferrosilite minerals in the original crushed/ground rock, and any other minerals/ores found in the original crushed/ground rock. In some embodiments, magnesium carbonate and silicon dioxide from the first reaction step can be separated from the residual iron silicate phases based on their respective densities. In one or more embodiments of these processes, the water that is added to the reactor 412 may have a low oxygen fugacity (e.g., it may be obtained from municipal wastewater treatment, groundwater, geothermal water, mine waters, another industrial water source, or by reacting a municipal water (i.e., “tap water”) over a bed of copper at temperatures exceeding 125° C., or by another mechanism) and a pH of between about 8.3 and about 11.1 (with the specified pH being artificially attained, such as by adding sodium bicarbonate to the water, or naturally obtained, such as where the water with such pH range may be found in certain sources of water and wastewater). During this second reaction step, the reactor is operated at a pre-selected temperature and pressure (˜1 to 20 bars) to facilitate the serpentinization of the fayalite and/or ferrosilite minerals in the rock. In one or more embodiments, the reactor 412 is operated at a temperature in the range of between about 80° C. and about 400° C. As provided in Table 1 above, the reaction of water with the fayalite (Fe2SiO4) and/or ferrosilite (Fe2Si2O6) produces hydrogen gas, variable mixtures of nitrogen (N2), carbon dioxide (CO2), silicon dioxide, and magnetite (Fe3O4) as reaction products. The molecular and isotopic composition of hydrogen formed during this ex situ process will be determined by the temperature conditions of the reaction (e.g., ˜175° C.) and the composition of the initial water, wherein the fractionation factors (a) between H2O and H2 follow the fractionation factors observed for standard geothermometers. The hydrogen gas, along with any other gases in the reactor 412, such as unreacted carbon dioxide (CO2), sulfur dioxide (SO2), or dihydrogen sulfide (H2S) or inert gases (e.g., nitrogen (N2), argon (Ar) from the first reaction step, are passed to a gas separator 414. The gas separator 414 may be a membrane unit, a pressure swing adsorption, or a cryogenic separation unit that can separate the hydrogen gas from other gases, e.g., atmospheric gases, that may also be present in the reactor 412. The gas separator 414 may be connected to and in fluid communication with at least one outlet of the reactor 412 and configured to separate hydrogen gas from gases that exit the reactor 412 through the at least one outlet.\|[0043] In at least one embodiment, gases that may be present in the reactor 412 prior to the second reaction may be evacuated prior to the second reaction, such as by pulling a vacuum on the reactor 412. Without these contaminant gases in the reactor 412 (e.g., N2 or CO2), the hydrogen gas that is formed as a result of the serpentinization reaction with water may be the only gas present after the second reaction step. In such case, the gas separator 414 may not be needed to segregate the hydrogen gas as a product. After the second reaction step, the magnesium carbonate, silicon dioxide, magnetite, and any remaining rock/unreacted ore may be removed from the reactor 412. In some embodiments, magnesium carbonate (i.e., magnesite) and silicon dioxide (i.e., quartz) may be separated from iron silicates and other mineral phases before the material is placed in reactor 412. The magnetite, which represents a valuable product/feedstock for the iron industry (with particular value in direct reduced iron manufacturing), may be recovered from the magnesium carbonate, silicon dioxide and any remaining rock/ore by, for example, magnetic separation or other density separation techniques. A magnetic separator 416 may be used to selectively attract the magnetite through the use of one or more magnets and thereby physically remove the magnetite from the other non-metallic ore. In one or more embodiments, the solid products, e.g., the magnetite, magnesium carbonate, silicon dioxide, and any remaining, unreacted ore/rock may be further crushed or ground (not shown in FIG. 4A) to facilitate the removal of magnetite particles from the other solids in the magnetic separator 416 or conduct secondary recovery of other minerals or metal-rich phases. The separated hydrogen gas from gas separator 414 and the magnetite recovered via the magnetic separator 416 are valuable products whose production and recovery from mafic and/or ultramafic rock are enhanced by the disclosed sequential carbonization and serpentinization reactions disclosed herein.\|[0044] The remaining magnesium carbonate (in which the carbon is permanently sequestered in the mineral phase), silicon dioxide, and any unreacted rock/ore may be used as an aggregate material and/or placed in landfill or otherwise disposed of. In one or more embodiments, the magnesium carbonate and silicon dioxide may be separated (based on density separation techniques such as heavy liquids or other gravity separation, or sluicing) and removed from the remaining rock/gangue (gangue: collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) materials. As further discussed below, magnesium carbonate (or magnesite) is useful in the manufacturing of pharmaceuticals, agricultural lime, and fertilizers (to neutralize acidification caused by fertilizer use), ceramics and ceramic brick, and as flux used in iron and steel manufacturing. Magnesite may also be used as a partial lime substitute to enable lower carbon emissions that result from the lower temperatures required to make magnesium oxide (MgO) as compared to calcium oxide (CaO) for cement manufacturing. Further, magnesite can be used as a carbon negative concrete filler and cement or aggregate substitute in concrete.\|[0045] In one or more embodiments, rather than landfilling or otherwise using the bulk of the magnesium carbonate, silicon dioxide, and any unreacted rock/ore, the rock and/or gangue material from the first reaction phase is further processed to separate and remove specific valuable components therefrom. For example, elevated concentrations of certain precious metals (e.g., nickel, cobalt, chromium, and rare earth elements) in mafic and ultramafic rocks are further concentrated in this “slag” material. In at least one embodiment, highly elevated metal enrichments, that include but are not limited to phosphates, aluminum oxides, precious metals, and other mineral gangue may be separated from the remaining rock/ore by, for instance, heavy liquid separation or other gravity separation, or sluicing in a separator 418. Through gravity separation, the various metals and other valuable components are ground into fine particles and separated based on their individual specific weights.\|[0046] As illustrated in FIG. 4A, the first and second reactions can both occur in the same reactor 412, which may be a rotary kiln, fluidized bed, toroidal bed, or other reactor as described previously, in which case the reactions may be run sequentially, and all products separated at the completion of both reactions. In one or more embodiments (not shown in FIG. 4A), the reaction products (i.e., magnesium carbonate and silicon dioxide) may be separated after the first reaction step and prior to the second reaction step using established density separation techniques such as heavy liquid separation or other gravity separation, or sluicing. In other embodiments, as shown in FIG. 4A, the reaction products remain in the reactor during the second reaction step. Even if the reaction products are not physically separated, the thermochemical activity and reaction rates of fayalite and/or ferrosilite will increase according to the newly exposed surface area of fayalite and/or ferrosilite minerals. In other words, the reactivity of the serpentinization reactions with respect to the fayalite and/or ferrosilite minerals will proceed according to the now higher molar fraction of fayalite and/or ferrosilite in the solid solution (i.e., the number and/or extent of alternative side reactions has been reduced). With respect to the upper limit of the fully separated (e.g., using established density separation techniques such as heavy liquid separation or other gravity separation, or sluicing) or exposed fayalite and/or ferrosilite, the thermochemical activity of the powdered material should approach unity of the pure phase mineral, or mixtures of fayalite and/or ferrosilite mineral phases. Thus, the first reaction step involving the reaction of the forsterite with carbon dioxide increases the thermochemical driver for the second reaction step, which is the serpentinization/hydration reaction of the fayalite and/or ferrosilite with water, by reducing the availability of forsterite and increasing the exposed surface area of fayalite and/or ferrosilite minerals. The former increases the kinetic rate by driving the thermochemical activity toward that of a pure compound, while the latter enhances chemical activity by increasing the surface area available for reaction.\|[0047] FIG. 4B illustrates a flow diagram of another embodiment 400″ of a system of enhancing the production of hydrogen gas and magnetite from a source rock that contains a mixture including olivine (fayalite and forsterite) and/or pyroxene (ferrosilite and enstatite) minerals. The flow diagram of FIG. 4B is similar to that of FIG. 4A, except that the first reaction step occurs in a first reactor 412′ and the second reaction step occurs in a second reactor 412″. The first reactor 412′ facilities the carbonation reaction between the forsterite mineral and carbon dioxide. The crushed/ground ore of a uniform or pre-selected particle size range is passed from the sieve 408 or other particle size separator into the first reactor 412′. Carbon dioxide is pumped into the first reactor 412′ in above stoichiometric ratios to facilitate the carbonization reactions listed in Table 2. After the first reaction has occurred, the magnesium carbonate and silicon dioxide products, along with the unreacted fayalite and/or ferrosilite, and other remaining ore, are passed to the second reactor 412″.\|[0048] Continuing with FIG. 4B, the second reactor 412″ facilitates the serpentinization reaction between the fayalite and/or ferrosilite mineral phases and water (or steam). The reaction products and remaining rock/ore from the first reactor 412′ are introduced into the second reactor 412″. Water is pumped into the second reactor 412″ in above stoichiometric ratios (>˜20 liters/kg of rock) to facilitate the serpentinization reactions listed in Table 1. After the second reaction has occurred, the reactor gases, including the hydrogen gas evolved during the second reaction step, are passed or routed to a gas separator 414, as described above with respect to FIG. 4A. Likewise, the solid reaction products, including magnesium carbonate, silicon dioxide, magnetite, as well as any unreacted ore/rock are passed to a magnetic separator 416, as described above with respect to FIG. 4B. Other than the use of two reactors 412′ and 412″ in place of one reactor 412, as described above, the embodiments represented by FIGS. 4A and 4B are similar. It should be noted that the configuration of the system of FIG. 4B provides a semi-continuous method in that the separate process vessels, e.g., reactors 412′ and 412″, are dedicated to differing portions of the method.\|[0049] FIGS. 5, 6, and 7 illustrate flowcharts of various embodiments for enhancing the production of hydrogen gas, magnetite, magnesite, and scarce metal resources from mafic and ultramafic igneous rock that contains a mixture of olivine (fayalite and forsterite) and pyroxene (ferrosilite and enstatite) minerals. As previously disclosed in connection with FIG. 3, olivine- and/or pyroxene-rich ores may be found in numerous locations around the world. At block 502, such olivine- and/or pyroxene-rich ore may be acquired from geological sites containing high concentrations of such rocks in one or more of these areas. FIG. 6 illustrates this rock acquisition operation in greater detail. As shown at block 602, the olivine- and/or pyroxene-rich source rock may be acquired in any manner known to those skilled in the art, such as by underground mining, strip mining, quarrying, outcrop quarrying, or the use of waste (i.e., mine tailings), etc. The source rock may be transported, e.g., by barge, train, truck, etc., to a facility to further process the rock. In one or more embodiments, the source rock may be processed in proximity to the location where the rock is acquired. The source rock may be processed by crushing and/or grinding the rock at block 606 into smaller size fractions. In addition to creating uniform or near uniform sizing, such comminution also helps to expose the minerals, such as olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite), that are contained within the rock. If the rock is processed in proximity to the geological site from which the rock originated, then the processed rock may then be transported to a facility having a system to further extract hydrogen, magnetite, and other valuable products from the ore according to a method disclosed herein (not shown in FIGS. 5 and 6). At block 608, the crushed and/or ground source rock may be further processed by sieving or otherwise segregating the rock according to size. In one or more embodiments, the crushed and/or ground rock may be washed with water or a slightly acidic solution to clean the surfaces thereof of dust, dirt, or other contaminants. As illustrated at block 604, such washing may be conducted before the rock is crushed and/or ground and can also benefit from agitation.\|[0050] The crushed and/or ground rock is then introduced into a reactor at block 610 in which the rock is reacted with carbon dioxide and water to produce magnesium carbonate and hydrogen gas, among other products, in stoichiometric proportions via the carbonation reactions described in Table 2. The crushed/ground rock may be transported between and introduced into the reactor at block 610 by conveyor, by machinery placement, etc. A slightly acidic water solution, as previously described may be applied, e.g., by washing, spraying, or soaking, onto the outer surfaces of the rock. Such application may be before or after the rock is deposited in the reactor. The air in the reactor, including oxygen therein, may be evacuated from the sealed reactor with the rock disposed therein (e.g., by applying a vacuum to the reactor) or purged using reaction gas (e.g., N2) prior to commencing the reaction. Returning to FIG. 5, block 504 describes that carbon dioxide (CO2) is introduced into the reactor to begin the first reaction phase. The carbon dioxide may be gaseous or supercritical as previously described. A greater-than-stoichiometric portion of carbon dioxide is added as compared to the amount of rock (and specifically forsterite concentration therein) in the reactor in order to ensure that the carbon dioxide does not limit the carbonation reaction and to benefit from increased reactivity that is observed to occur at elevated pressures of CO2 and/or super-critical CO2. At block 504, the reactor is operated at one or more pre-selected temperatures and pressures, as described above, for a first residence time in order to sufficiently react the carbon dioxide with the forsterite mineral to produce magnesium carbonate and silicon dioxide reaction products. At the end of the first residence time, the gas phase from the reactor may be evacuated by, e.g., applying a vacuum or gas purging operation, to remove the excess unreacted carbon dioxide and any other gases evolved via the carbonation reactions of the first reaction phase.\|[0051] Continuing with FIG. 5, at block 506, water is introduced to the reactor after the first residence time. In one or more embodiments, the water is a low oxygen fugacity water that is prepared or obtained as described in greater detail above. Again, a greater-than-stoichiometric portion of water (>˜20 liters/kg of rock) is added as compared to the amount of rock (and specifically fayalite and/or ferrosilite concentrations therein) in the reactor in order to ensure that the water does not limit the serpentinization reaction. At block 506, the reactor is operated at one or more pre-selected temperatures and pressures, as described above, for a second residence time in order to sufficiently react the water with the fayalite and/or ferrosilite minerals (now having additional exposed surface area and more optimized chemical activity due to the first reaction phase) to produce at least hydrogen gas and magnetite reaction products.\|[0052] At block 508, the gas phase is removed from the reactor either during or at the completion of the second reaction phase. This gas phase, which is rich in hydrogen gas (and may contain small quantities of trace gases, e.g., N2, Ar, CO2) may be further purified through gas separator 414 (as shown in FIG. 4A and FIG. 4B). The gas separator 414 may be a pressure swing adsorption unit, a membrane separation unit, a cryogenic separation unit, or any other gas separation unit known to those skilled in the art. If the gas phase was not evacuated from the reactor between the first reaction phase and the second reaction phase, then some carbon dioxide and/or other gases, e.g., reaction gases, may contaminate the hydrogen gas evolved in the reactor via the serpentinization reactions of the second reaction phase.\|[0053] At block 510, the remaining rock within the reactor may be further processed to remove the magnesium carbonate/magnesite, the iron oxide/magnetite, the silicon dioxide, any remaining ore and/or slag material from the reactor. These operations are described in detail in connection with FIG. 7. Block 702 illustrates that the remaining rock in the reactor may be removed for further processing. Such removal may include removal by mechanical machinery, which picks up, rakes, or gravity feeds the material from the reactor into a container or onto a conveyor. In particular, at block 702 the solid reaction products (i.e., magnesite, magnetite, etc.), the remaining ore, and any slag material may be passed to a magnetic separator 416 (as shown in FIG. 4A and FIG. 4B) in order to separate the magnetite from the other materials via attraction of the magnetically susceptible iron oxide to a magnetic field (see block 704). The solid material removed from the reactor at block 702 may undergo additional crushing and/or grinding in order to create a fine powder to facilitate removal of valuable components thereof (not shown in FIGS. 5 and 7). At block 706, any precious or scarce metals that are now more concentrated in the remaining ore and/or gangue (collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) material after magnetite removal may be separated and removed based on density separation techniques such as heavy liquid separation or other gravity separation, or sluicing; an example of gravity separation using a gravity separator is shown in 480. Finally, as shown in block 708, the remaining rock, containing remaining magnesium carbonate (in which the carbon is permanently sequestered in the mineral phase), silicon dioxide, and any unreacted rock/ore may be used as an aggregate material and/or placed in landfill or otherwise disposed of. As noted previously, in some embodiments the magnesium carbonate and silicon dioxide may be separated (based on density separation techniques such as heavy liquids separation, or other gravity separation, or sluicing) and removed from the remaining rock/gangue (gangue: collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) materials for separate dispositioning.\|[0054] FIGS. 5, 6, and 7 illustrates operations performed in various example embodiments. It will be understood that each flowchart block, and each combination of flowchart blocks, may be implemented by various means. The flowchart blocks support combinations of means for performing the specified functions and combinations of operations for performing the specified functions. In some embodiments, some of the operations above may be modified or further amplified. Furthermore, in some embodiments, additional optional operations may be included. Modifications, amplifications, or additions to the operations above may be performed in any order and in any combination.	(US12545576)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This application is a continuation of U.S. application Ser. No. 18/302,702 filed Apr. 18, 2023, which is a continuation of U.S. patent application Ser. No. 17/815,914 filed Jul. 28, 2022, which claims the benefit of U.S. Provisional Patent Application No. 63/203,814 filed Jul. 30, 2021. The entire contents of all of the above applications are incorporated herein by reference.\|(US12545576)\|FIELD OF THE DISCLOSURE\|[0002] One or more embodiments of this disclosure generally relate to systems and methods that produce hydrogen, generate magnetite, and/or derive additional desired products from ores containing olivine or pyroxene (such as mafic and/or ultramafic rocks) through pre-selected chemical processes. In one or more embodiments, the systems and methods facilitate carbonization and/or serpentinization/hydration reactions involving olivine- and pyroxene-rich ores in order to sequester carbon dioxide, liberate hydrogen, generate magnetite and magnesite, and/or derive other desired products, including scarce metals, which are in many cases critical to various green technologies (e.g., batteries, energy storage, photovoltaics) otherwise mined using carbon-intensive methods.\|BACKGROUND\|[0003] The environmental impact of greenhouse gases, primarily carbon dioxide (CO2) and methane (CH4), has been the subject of much public debate over the past several decades. More recently, self-imposed private-sector initiatives and government-mandated regulations to reduce the release of greenhouse gases into the environment have begun to be implemented. In addition to the capture and/or sequestration of carbon dioxide and other greenhouse gases to mitigate their atmospheric release, much research and development effort has been focused on the utilization of alternatives to fossil fuel combustion for energy production in order to reduce the amount of carbon dioxide generated and/or that must be captured and sequestered.\|[0004] Hydrogen (H2) gas holds promise as an energy source (e.g., as hydrogen fuel or through the use of green ammonia) and chemical feedstock (e.g., methanol, ammonia, hydrocarbon fuels) that provides little-to-no greenhouse gas emission upon combustion. Indeed, the combustion of hydrogen gas yields just water as a reaction product. However, hydrogen gas has traditionally been produced using fossil fuels (e.g., via natural gas/methane conversion in a steam reformer), which yields the greenhouse gas carbon dioxide as a reaction product. For example, in the steam-methane reforming reaction mentioned, methane is reacted with steam (i.e., water) to produce hydrogen gas and carbon monoxide. In a subsequent water-gas shift reaction, the carbon monoxide is further reacted with steam to produce carbon dioxide and additional hydrogen gas. The hydrogen gas is subsequently separated from the carbon dioxide through pressure swing adsorption, membrane separation, or another gas separation process. Thus, most hydrogen that is produced in refinery operations, for example, produces greenhouse gases, which must be captured and sequestered to yield meaningful benefit.\|[0005] Alternatively, hydrogen gas may be generated by the electrolysis of water into hydrogen gas and oxygen. The hydrogen gas is subsequently separated from oxygen through pressure swing adsorption, membrane separation, or another gas separation process. Hydrogen production via electrolysis, or partial pyrolysis reactions, requires a substantial amount of electricity. While at least some of the required electricity for hydrogen production via electrolysis and/or partial pyrolysis reactions may be obtained from renewable sources (e.g., wind, solar, and hydroelectric), in practice the majority of the electricity used for this purpose has traditionally been, and continues to be, produced through the combustion of fossils fuels, which also produces greenhouse gases.\|[0006] The abiotic production of hydrogen gas is known to occur in certain geological formations, e.g., at young oceanic crust near a mid-oceanic ridge, as depicted in FIGS. 1A-1D. These natural reactions occur across a range of environmental conditions that include variable pH, oxygen fugacity, chemical composition, and pressure. Such reactions produce variable and complex mineralogy and chemistry but do not predictably produce any specific combination of reaction products. In fact, as generally illustrated in the cross-section photograph of FIG. 2, rock deposits 200 that may yield abiotic hydrogen often contain complex mixtures or layers of difficult-to-extract mineral phases, or will not produce a desired product if other competing reactions are preferred based on in situ geochemical conditions (e.g., variable redox potential (Eh), pH, pore water composition, gas chemical composition, and temperature). For example, hydrogen production is highly variable in nature and its occurrence greatly depends on pH, Eh, and other aspects of fluid geochemistry in pore spaces and at mineral surfaces. Thus, the complex kinetics of reaction phases and the occurrence of competing reactions in natural conditions (e.g., circumneutral pH, variable oxygen fugacity, and variable pore water chemistry) govern the products yielded by these naturally occurring reactions. Certain geological formations and/or the rocks thereof are also known to contain minerals that are conducive to reaction with carbon dioxide under certain conditions to form carbonated mineral phases, e.g., carbonates.\|BRIEF SUMMARY\|[0007] FIG. 3 provides a map that highlights the example locations of selected suitable and/or robust deposits of mafic and ultramafic rock around the world. Olivine- and pyroxene-bearing ores may be found in such mafic and/or ultramafic formations. As can be understood from FIG. 3, sources of mafic and ultramafic igneous rocks may be found in many locations and are quite plentiful, accounting for at least 10% of the continental crust of the Earth, which illustrates the global applicability of solutions described herein. More recently, such sources of mafic and ultramafic igneous rock have garnered interest for their potential exploitation to sequester (mineralize) carbon dioxide in carbonate mineral phases. However, despite significant prior work on carbon sequestration, there is considerable debate about the best mechanistic reactions and optimized rates for carbon mineralization. As such, the economic viability of these processes has not been fully developed, nor has the hydrogen generation and carbon sequestration capacity of mafic and ultramafic rocks been realized. Moreover, no economic use has been identified for the fine-grained carbonated mineral phases that result from carbonization reactions. Rather, proposals have recommended such carbonated mineral phases be used as fill or dumped in oceans or lakes).\|[0008] Despite the theoretical potential for such geological formations and/or the ores thereof to be exploited for geological hydrogen or other products, and for potential carbon sequestration, the processes and kinetics of these reactions has not been rigorously evaluated nor optimized. Further, processes for the production of hydrogen from these geological formations without the occurrence of alternative, and sometimes deleterious, mineral phases (e.g., serpentine, such as antigorite, asbestos) have not been developed. Accordingly, Applicant has recognized a need for systems and methods that exploit certain geological formations and/or the ores thereof to liberate hydrogen, generate magnetite and magnesite, and/or derive other desired products, such as scarce/critical metals from geological formations that include olivine- and pyroxene-rich ores, and in addition, sequester carbon dioxide in magnesite or other mineral phases.\|[0009] The disclosure herein provides one or more embodiments of systems and methods for sequestering carbon, evolving hydrogen gas, and producing magnetite as well as magnesite from olivine- and pyroxene-bearing ores. In addition, precious or scarce metals, such as nickel, cobalt, chromium, and rare earth elements, may be concentrated in the remaining ore, which facilitates their recovery.\|[0010] In an example embodiment, a method is provided for sequestering carbon and producing hydrogen and magnetite. The method includes obtaining an ore that containing olivine or pyroxene. The ore may be comminuted into smaller size fractions, such as by crushing or grinding. The comminuted ore may be introduced into a reactor that is operable at temperatures above ambient temperature and pressures above atmospheric pressure. The method may also include introducing carbon dioxide (or a mixture of carbon dioxide and other gases such as nitrogen (N2), dihydrogen sulfide (H2S), and sulfur dioxide (SO2) into the reactor at a first temperature above ambient temperature for a first residence time to react at least a portion of the carbon dioxide with the ore. The method also includes later introducing water into the reactor at a second temperature for a second residence time to react at least a portion of the water with one or more of the remaining ore to generate at least magnetite and hydrogen gas. Reaction products, including hydrogen gas, magnesium carbonate (magnesite), magnetite, other reaction products, and any remaining ore may be removed from the reactor.\|[0011] In another embodiment, a method is provided for sequestering carbon and generating hydrogen and magnetite from rock. The method includes obtaining an ore that olivine or pyroxene. As above, the ore may be broken down into smaller size fractions, such as by crushing or grinding. The ore is introduced into a first reactor that is operable at a first temperature above ambient temperature and pressures above atmospheric pressure. The method also includes introducing carbon dioxide (or a mixture of carbon dioxide and other gases such as nitrogen (N2), dihydrogen sulfide (H2S), and sulfur dioxide (SO2)) into the first reactor at the first temperature for a first residence time to react at least a portion of the carbon dioxide with the ore to generate at least magnesium carbonate. The remaining ore may be passed to a second reactor. Reaction products from the first reactor may be separated from the remaining ore or may also be passed to the second reactor. The method also includes introducing water into the second reactor at a second temperature for a second residence time to react at least a portion of the water with the remaining ore in the second reactor to produce at least magnetite and hydrogen gas. Reaction products, including hydrogen gas, magnesium carbonate (magnesite), magnetite, other reaction products and any remaining ore may be removed from the second reactor.\|[0012] In yet another embodiment, a system is provided for sequestering carbon and producing hydrogen and magnetite from rock. The system includes a source of ore that contains olivine or pyroxene. The system may include a crusher or grinder used to physically reduce the particle size of the ore introduced therein from the source. The system may include a sieve used to receive the ore from the crusher and configured to allow ore particles up to a pre-selected size to pass therethrough. The system also includes a reactor having an inlet that receives ore particles up to the pre-selected size from the sieve and at least one outlet. The reactor also has at least one additional inlet through which one or more of carbon dioxide or water may be introduced (and in some embodiments, the reactor may comprise two reactors: a first reactor having an additional inlet through which carbon dioxide may be introduced, and a second reactor having another additional inlet through which water may be introduced). The reactor is operable at a first temperature for a first residence time to react at least a portion of any received carbon dioxide with the ore in the first reactor to generate at least magnesium carbonate. The reactor is also operable at a second temperature for a second residence time to react at least a portion of any water that enters the reactor through the at least one additional inlet with any ore within the reactor to generate magnetite and hydrogen gas. In one or more embodiments, the system also includes a gas separator that is connected to and in fluid communication with the at least one outlet of the reactor. The gas separator is configured to separate hydrogen gas from gases that exit the reactor through at least one outlet of the reactor.\|[0013] Corresponding means for performing these various steps are set forth below.\|[0014] The foregoing brief summary is provided merely for purposes of summarizing some example embodiments described herein. Because the above-described embodiments are merely examples, they should not be construed to narrow the scope of this disclosure in any way. It will be appreciated that the scope of the present disclosure encompasses many potential embodiments in addition to those summarized above, some of which will be described in further detail below.\|(US12545576)\|BRIEF DESCRIPTION OF THE FIGURES\|[0015] Having described certain example embodiments in general terms above, reference will now be made to the accompanying drawings, which are not necessarily drawn to scale. Some embodiments may include fewer or more components than those shown in the figures.\|[0016] FIGS. 1A, 1B, 1C, and 1D illustrate cross-sectional representations of young oceanic crust and associated structures positioned near a theoretical mid-oceanic ridge that may produce and/or host abiotic hydrogen production.\|[0017] FIG. 2 illustrates an example cross-section of serpentinized ultramafic rock.\|[0018] FIG. 3 illustrates a map with locations of suitable olivine- and pyroxene-bearing localities throughout the world.\|[0019] FIG. 4A provides an example flow diagram illustrating a sequence of operations performed by a system to enhance carbon dioxide sequestration, hydrogen gas evolution, and magnetite and magnesite production using a single reactor, in accordance with some example embodiments described herein.\|[0020] FIG. 4B provides an example flow diagram illustrating a sequence of operations performed by a system to enhance carbon dioxide sequestration, hydrogen gas evolution, and magnetite/magnesite production using multiple reactors, in accordance with some example embodiments described herein.\|[0021] FIG. 5 illustrates an example flowchart for enhancing carbon dioxide sequestration, hydrogen gas evolution, and magnetite/magnesite production, in accordance with some example embodiments described herein.\|[0022] FIG. 6 illustrates an example flowchart for acquisition and preparation of source rock for reaction, in accordance with some example embodiments described herein.\|[0023] FIG. 7 illustrates an example flowchart for processing rock remaining following any carbon dioxide and/or water reactions, in accordance with some example embodiments described herein.\|(US12545576)\|DETAILED DESCRIPTION\|[0024] Some example embodiments will now be described more fully hereinafter with reference to the accompanying figures, in which some, but not necessarily all, embodiments are shown. Because inventions described herein may be embodied in many different forms, the invention should not be limited solely to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will satisfy applicable legal requirements.\|Overview\|[0025] Applicant recognized that despite the significant theoretical potential of mafic and/or ultramafic igneous rocks (or, more broadly, olivine- and pyroxene-bearing ores, such as those with elevated iron content), as described above, to serve as geological sources for economic geological hydrogen, to be exploited as natural sources and catalysts for hydrogen and magnetite production, and to be exploited for carbon sequestration, the optimal processes and kinetics for these reactions have not been rigorously evaluated nor optimized. Specifically, process steps to enhance both carbon sequestration and the production of hydrogen, magnetite, magnesite, and/or other minerals from these types of rocks—without the formation of alternative (and sometimes deleterious, e.g., serpentine, asbestos) mineral phases—have not been developed.\|[0026] Further, Applicant is unaware of any prior attempts to use an optimized chemical process of carbon mineralization to enhance the kinetics of hydrogen and magnetite production, or to regulate the chemical species of the resulting reaction products (e.g., prevent the formation of serpentine and asbestos).\|[0027] In various embodiments disclosed herein, carbon dioxide may be sequestered, and hydrogen, magnetite, and other scarce metals may be produced economically (and with a neutral to net-negative carbon footprint) using olivine- and pyroxene-rich ores through sequential carbonation and serpentinization reactions in a controlled environment. Thus, Applicant has developed an engineering process that employs sequential reactions to exploit the potential for olivine- and pyroxene-rich ores to both sequester carbon dioxide dominantly as magnesite or other carbonate minerals, as well as liberate hydrogen, magnetite, and/or other desirable minerals/scarce metals. Applicant further recognized that additional process steps applied to the olivine- and pyroxene-rich ores may enhance the concentration and recovery of precious or scarce metals (e.g., nickel, cobalt, chromium, lithium, and rare earth elements.), which are needed for renewable energy and energy storage, among other uses.\|[0028] Applicant discovered that the serpentinization reaction process can be advantaged such that the chemical activity and commensurate rates of reactions between water and fayalite and/or ferrosilite may be enhanced by first removing a significant component of forsterite from the olivine mineral phase and increasing the comminution of mineral grains by inducing the described chemical reactions. In this way, the fayalite and/or ferrosilite in the igneous rock is concentrated and/or becomes less obscured by adjacent minerals, e.g., forsterite. This process benefits the reaction in two ways: first, by enhancing the surface area of fayalite and/or ferrosilite exposed for the reaction; and second, by pre-concentrating the reactant (iron-rich olivine (fayalite) or pyroxene (ferrosilite)) of choice. Thus, in one or more embodiments, forsterite and/or enstatite are at least partially removed prior to reacting the fayalite and/or ferrosilite with water.\|[0029] Some primary differentiators that demonstrate the value of example ex situ engineered embodiments that produce hydrogen, magnesite, magnetite, and critical metals via this pathway include: 1) the immense geological scalability of such embodiments once the “serpentinization” processes are optimized to produce the desired products (hydrogen, magnetite, scarce metals), as opposed to alternative mineral phases such as serpentine, asbestos, etc.; 2) the potential to permanently and verifiably sequester CO2 in a mineralized form and hence produce hydrogen, magnetite, and scarce metals in a carbon-negative process; and 3) the price point of potentially scalable “green” or “golden” hydrogen (i.e., carbon negative hydrogen), magnetite, and scarce metals, which can be greatly offset by considering other values streams generated using the quarrying concept (i.e., the sale of aggregate or higher value utilization of magnesite).\|[0030] Although a high-level explanation of the operations of example embodiments has been provided above, specific details regarding the configuration of such example embodiments are provided below.\|Serpentinization and Carbonation Reactions\|[0031] The disclosure herein provides one or more embodiments of systems and methods that facilitate the production of hydrogen, magnetite, and/or other desired minerals through serpentinization reactions involving olivine- and pyroxene-rich ores generally found in mafic and/or ultramafic igneous rock, or of any other rock assemblages containing such olivine- and pyroxene-rich ores. Table 1, provided below, gives representative serpentinization reactions involving fayalite (Fe2SiO4) and/or ferrosilite (Fe2Si2O6). Fayalite is a mineral phase that is the iron-rich endmember of the olivine solid solution series and is abundant in olivine-rich orc. Ferrosilite is the iron-rich endmember of the orthopyroxene solid solution series and is associated with pyroxene-rich ore. Fayalite and ferrosilite are commonly found together in mafic and ultramafic igneous rocks. Under certain conditions, water reacts with fayalite and ferrosilite to generate magnetite (Fe3O4), silica (SiO2), and hydrogen gas (H2) in the appropriate stoichiometric ratios. In each case, two moles of hydrogen gas are produced from three moles of either fayalite or ferrosilite mineral.\|[0032] TABLE 1 Hydrogen-Generating Serpentinization ReactionsSerpentinization Reactions Moles of MineralSerpentinizationIgneousMolesMineralPhaseReactionMineralof H2 OlivineFayalite3 Fe2 + 2 H2O →32 2 Fe3O4 + 3 SiO2 + 2 H2 PyroxeneFerrosilite3 Fe2Si2O6 + 2 H2O →32 2 Fe3O4 + 6 SiO2 + 2 H2 \|[0033] In one or more embodiments, the disclosed systems and methods may also facilitate the sequestration of gaseous carbon dioxide as mineralized carbonates through carbonation reactions involving the magnesium-rich endmember of olivine- and pyroxene-rich ores found typically in mafic and/or ultramafic rock. Table 2, provided below, gives representative carbonation reactions involving forsterite (Mg2SiO4) and enstatite (Mg2Si2O6), as well as illustrating the potential for carbonation during reaction with antigorite (Mg3Si2O5(OH)4) that can be formed as an accessory mineral phase in natural systems in which fluid conditions are not idealized for the formation of magnesite. Forsterite is a mineral phase that is the magnesium-rich endmember of the olivine solid solution series associated with olivine-rich ore. Enstatite is a mineral phase that is the magnesium-rich endmember of the orthopyroxene solid solution series associated with pyroxene-rich ore. Antigorite is an example mineral phase that is associated with serpentine. Under certain conditions, carbon dioxide reacts with forsterite and enstatite, and/or other accessory mineral phases (e.g., antigorite) to generate at least magnesium carbonate (MgCO3) and silica (SiO2) in appropriate stoichiometric ratios. The reaction of antigorite with carbon dioxide further yields a stoichiometric quantity of water and is shown to illustrate serpentinization reactions that occur in natural systems in which pH, Eh, temperature, pressure, and fluid chemistry cannot be optimized. In the case of the idealized carbonization reaction involving forsterite and enstatite, two moles of carbon dioxide gas are converted to magnesium carbonate (magnesite) per mole of either forsterite or enstatite mineral.\|[0034] TABLE 2 Carbon-Sequestering Carbonation ReactionsDecarbonation Reactions Moles of MineralDecarbonationIgneousMolesMineralPhaseReactionMineralof CO2 OlivineForsteriteMg2SiO4 + 2 CO2 →12 2 MgCO3 + SiO2 PyroxeneEnstatiteMg2Si2O6 + 2 CO2 →12 2 MgCO3 + 2 SiO2 SerpentineAntigoriteMg3Si2O5(OH)4 +13 3 CO2 → 3 MgCO3 + 2 SiO2 + 2 H2O \|[0035] In nature, and as previously described, the above-described serpentinization and carbonization reactions occur, but only as a subset of a variety of reactions occurring across a range of environmental conditions in the subsurface or at surface conditions of the earth. As a result, the environmental conditions are often variable and reactions kinetics and pathways are far from ideal. Accordingly, natural reactions are based on the variable (and often dynamic, i.e., changing with time) pH, oxygen fugacity, temperature, pore water chemical composition, gas chemical composition, and pressure found in nature, specifically in the subsurface. The multitude of reactions and potential pathways for those reactions occurring in nature lead to the formation of variable and complex chemistry and assemblages of minerals, but do not predictably produce any specific combination of usable reaction products. Instead, natural systems, which evolve through time and under varying reaction conditions produce complex (and often heterogeneous) complexes of varying mineral assemblages and products of reactions that did not follow the idealized reactions described above, or are slower to reach thermodynamic equilibrium.\|[0036] With respect to olivine and pyroxene mineralogy and chemistry, olivine is a solid solution series (X2SiO4, where X═Mg2+ or Fe2+) between a magnesium silicate (forsterite) and an iron silicate (fayalite) and pyroxene (i.e., orthopyroxene) is a solid solution series (X2Si2O6, where X═Mg2+ or Fe2+) between a magnesium silicate (enstatite) and an iron silicate (ferrosilite). In the olivine-rich deposits of interest, fayalite and ferrosilite are usually the minor constituent and typically range in concentration from 6% to 20%, with the lower range concentrations appearing more commonly in nature. Consequently, the thermochemical activities of fayalite and ferrosilite are relatively low compared to those of the forsterite or enstatite, respectively. Thus, if the olivine or pyroxene obtained from a quarry is crushed and reacted with water at favorable reaction conditions (i.e., controlled for temperatures, pressures, Eh, pH, and fluid composition, then a serpentinization reaction will proceed at a relatively low rate due to relatively low thermochemical activity and commensurately low rates of reactions with fayalite or ferrosilite. Nevertheless, when completed, the reaction produces magnetite, silica, and hydrogen (from the reaction of fayalite or ferrosilite with water) may be separated (magnetically or gravimetrically) from forsterite, enstatite, or magnesite. The mixture of olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite) minerals, however, constitutes an almost an “ideal” mixture that is exceedingly rare in natural systems. However, in an ideal mixture, the chemical activity varies linearly with the mole fraction and is roughly equal to the mole fraction. Thus, the chemical activity and reaction rate can be enhanced by pre-concentrating the abundance of olivine and pyroxene from the bulk ore and specifically the abundance of the iron-rich endmembers of both the olivine and pyroxene solid solution series.\|Ex Situ Sequestration of Carbon Dioxide and Generation of Hydrogen\|[0037] In various embodiments contemplated herein, carbon dioxide may be mineralized, and hydrogen, magnesite, magnetite, and critical metals may be produced economically (and with an overall neutral to net-negative carbon footprint) by an engineered system that causes sequential reactions in the manner shown in the flow diagrams illustrated in FIGS. 4A, 4B, and described in connection with the flowcharts provided in FIGS. 5, 6, and 7.\|[0038] FIG. 4A illustrates a flow diagram of one embodiment 400′ of a system for enhancing the production of hydrogen gas and magnetite from rock that contains a mixture of olivine (e.g., fayalite and forsterite) and pyroxene (e.g., ferrosilite and enstatite) minerals. A source of olivine- and/or pyroxene-rich ores 402 may be fed or introduced into a crusher or grinder 406 that reduces the size of the received ore into smaller size fractions. In one or more embodiments, a washer 404 may optionally be used to wash the ore with water or a mildly acidic solution to remove any contaminants therefrom and prepare the ore for carbonation reactions. The crushed or ground rock is then introduced into a sieve 408 or other such separator that segregates the rock into pre-selected particle ranges. In one or more embodiments, the sieves or grates thereof are sized to pass 150-, 80-, and even 45-micron grains, although different sizing can be utilized. In at least one embodiment, the comminuted rock is a powder or has a powder-like particle size range. Rock that does not pass through the sieve may be returned to the crusher or grinder 406 via a recycle loop 410 to be reduced further in size. The subset of the rock having particles within a pre-selected particle range of the sieve 408, e.g., 150-micron, 80-micron, 45-micron, or any size therebetween, is then fed or introduced into a reactor 412.\|[0039] The reactor 412 may be a rotary kiln, a toroidal fluidized bed, a fluidized bed, or another reactor known to those skilled in the art. The reactor 412 may have an inlet that receives ore (or ore particles) at least one outlet, from which any remaining ore may be removed following reaction within the reactor 412. The reactor 412 may further have at least one additional inlet through which one or more of carbon dioxide or water can be introduced into the reactor 412. The reactor 412 may be operable at a first temperature for a first residence time to react carbon dioxide that enters the reactor 412 through the at least one additional inlet with ore disposed within the reactor 412 to generate magnesium carbonate. The reactor 412 may further be operable at a second temperature for a second residence time to react water that enters the reactor through the at least one additional inlet (which may be the same inlet by which carbon dioxide enters the reactor 412 or a different inlet) with ore disposed within the reactor 412 to generate magnetite and hydrogen gas.\|[0040] In a first reaction step, carbon dioxide is introduced into reactor 412 with the crushed/ground rock. Water (approximately 10 liters of water per kilogram) may be applied (sprayed or washed) to the crushed/ground rock by washer 404 either before or after placement of the rock into the reactor 412. The wetting of the powdered rock with water allows for the dissolution of gaseous CO2 to carbonic acid (H2CO3) on the wet surfaces of the mineral grains, which enhances the reactivity of the carbon dioxide with the forsterite mineral found therein. In at least one embodiment, the pH of the water applied to the comminuted rock may be between about 4.8 to about 6.5. Water in this pre-selected pH range further enhances the reaction between the carbon dioxide and the forsterite mineral. During this first reaction step, the reactor is operated at a pre-selected temperature (>90° C.) and pressure (greater than approximately five bars) to facilitate the carbonation reaction with respect to the forsterite mineral found in the rock. In one or more embodiments, the reactor 412 is operated at a temperature of between about 100° C. to about 400° C. and at a pressure of between about five and up to at least 100 bars (e.g., about 40, 50, 75 or even 100 bars); note the upper limit of pressure can be extended to considerably higher pressures if the reactor 412 and associated components are able to withstand such pressures. Increasing pressure in this fashion will produce a corresponding enhancement of the carbonation reaction being prompted at this stage of the process. In other embodiments, the operating pressure of the reactor 412 may be as low as 35 bars, as low as 30 bars, as low as 25 bars, as low as 20 bars, as low as 15 bars, as low as 10 bars, as low as 5 bars, or even lower (˜1 bar), and may still prompt the intended carbonation reactions, albeit at commensurately lower rates of reaction. As provided in Table 2 above, the reaction of carbon dioxide with the forsterite (Mg2SiO4) produces magnesium carbonate (MgCO3) and silicon dioxide (SiO2) as reaction products. In this way, the forsterite mineral of the mafic and/or ultramafic rock is used to permanently sequester CO2 in the form of an insoluble magnesium carbonate mineral lattice, which is a solid that that can be useful as a raw material, placed in a landfill, ocean, lake, or otherwise easily stored. By reacting the crushed/ground rock containing the forsterite with carbon dioxide at favorable conditions of temperature, pressure, Eh, and pH, the forsterite can be altered to magnesite following reaction with carbon dioxide.\|[0041] It will be understood that, although this first reaction step favorably enhances the comminution of source rock and better prepares any remaining rock for the second reaction step described below, some embodiments may not perform this first reaction step, and instead may simply comminute the source rock, which itself prepares the source rock for the second reaction step, as illustrated by way of example in the Example Implementation section below. Of course, in other embodiments, the source rock may not need to undergo an initial comminution step, but may instead simply be initially processed using the first reaction step described herein, which itself fosters comminution of the source rock and thus prepares it for more effective reaction in the second reaction step described below. Both comminution of the source rock and the carbonation reactions occurring during the first reaction step favorably dispose any remaining rock for the section reaction step below; accordingly, various combination of comminution and the first reaction step may be employed in various scenarios based on the desired results of a given implementation.\|[0042] In a second reaction step, water is thereafter introduced into reactor 412 with the crushed/ground rock, which may in some embodiments still contain the magnesium carbonate and silicon dioxide from the first reaction step, the fayalite and/or ferrosilite minerals in the original crushed/ground rock, and any other minerals/ores found in the original crushed/ground rock. In some embodiments, magnesium carbonate and silicon dioxide from the first reaction step can be separated from the residual iron silicate phases based on their respective densities. In one or more embodiments of these processes, the water that is added to the reactor 412 may have a low oxygen fugacity (e.g., it may be obtained from municipal wastewater treatment, groundwater, geothermal water, mine waters, another industrial water source, or by reacting a municipal water (i.e., “tap water”) over a bed of copper at temperatures exceeding 125° C., or by another mechanism) and a pH of between about 8.3 and about 11.1 (with the specified pH being artificially attained, such as by adding sodium bicarbonate to the water, or naturally obtained, such as where the water with such pH range may be found in certain sources of water and wastewater). During this second reaction step, the reactor is operated at a pre-selected temperature and pressure (˜1 to 20 bars) to facilitate the serpentinization of the fayalite and/or ferrosilite minerals in the rock. In one or more embodiments, the reactor 412 is operated at a temperature in the range of between about 80° C. and about 400° C. As provided in Table 1 above, the reaction of water with the fayalite (Fe2SiO4) and/or ferrosilite (Fe2Si2O6) produces hydrogen gas, variable mixtures of nitrogen (N2), carbon dioxide (CO2), silicon dioxide, and magnetite (Fe3O4) as reaction products. The molecular and isotopic composition of hydrogen formed during this ex situ process will be determined by the temperature conditions of the reaction (e.g., ˜175° C.) and the composition of the initial water, wherein the fractionation factors (a) between H2O and H2 follow the fractionation factors observed for standard geothermometers. The hydrogen gas, along with any other gases in the reactor 412, such as unreacted carbon dioxide (CO2), sulfur dioxide (SO2), or dihydrogen sulfide (H2S) or inert gases (e.g., nitrogen (N2), argon (Ar) from the first reaction step, are passed to a gas separator 414. The gas separator 414 may be a membrane unit, a pressure swing adsorption, or a cryogenic separation unit that can separate the hydrogen gas from other gases, e.g., atmospheric gases, that may also be present in the reactor 412. The gas separator 414 may be connected to and in fluid communication with at least one outlet of the reactor 412 and configured to separate hydrogen gas from gases that exit the reactor 412 through the at least one outlet.\|[0043] In at least one embodiment, gases that may be present in the reactor 412 prior to the second reaction may be evacuated prior to the second reaction, such as by pulling a vacuum on the reactor 412. Without these contaminant gases in the reactor 412 (e.g., N2 or CO2), the hydrogen gas that is formed as a result of the serpentinization reaction with water may be the only gas present after the second reaction step. In such case, the gas separator 414 may not be needed to segregate the hydrogen gas as a product. After the second reaction step, the magnesium carbonate, silicon dioxide, magnetite, and any remaining rock/unreacted ore may be removed from the reactor 412. In some embodiments, magnesium carbonate (i.e., magnesite) and silicon dioxide (i.e., quartz) may be separated from iron silicates and other mineral phases before the material is placed in reactor 412. The magnetite, which represents a valuable product/feedstock for the iron industry (with particular value in direct reduced iron manufacturing), may be recovered from the magnesium carbonate, silicon dioxide and any remaining rock/ore by, for example, magnetic separation or other density separation techniques. A magnetic separator 416 may be used to selectively attract the magnetite through the use of one or more magnets and thereby physically remove the magnetite from the other non-metallic ore. In one or more embodiments, the solid products, e.g., the magnetite, magnesium carbonate, silicon dioxide, and any remaining, unreacted ore/rock may be further crushed or ground (not shown in FIG. 4A) to facilitate the removal of magnetite particles from the other solids in the magnetic separator 416 or conduct secondary recovery of other minerals or metal-rich phases. The separated hydrogen gas from gas separator 414 and the magnetite recovered via the magnetic separator 416 are valuable products whose production and recovery from mafic and/or ultramafic rock are enhanced by the disclosed sequential carbonization and serpentinization reactions disclosed herein.\|[0044] The remaining magnesium carbonate (in which the carbon is permanently sequestered in the mineral phase), silicon dioxide, and any unreacted rock/ore may be used as an aggregate material and/or placed in landfill or otherwise disposed of. In one or more embodiments, the magnesium carbonate and silicon dioxide may be separated (based on density separation techniques such as heavy liquids or other gravity separation, or sluicing) and removed from the remaining rock/gangue (gangue: collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) materials. As further discussed below, magnesium carbonate (or magnesite) is useful in the manufacturing of pharmaceuticals, agricultural lime, and fertilizers (to neutralize acidification caused by fertilizer use), ceramics and ceramic brick, and as flux used in iron and steel manufacturing. Magnesite may also be used as a partial lime substitute to enable lower carbon emissions that result from the lower temperatures required to make magnesium oxide (MgO) as compared to calcium oxide (CaO) for cement manufacturing. Further, magnesite can be used as a carbon negative concrete filler and cement or aggregate substitute in concrete.\|[0045] In one or more embodiments, rather than landfilling or otherwise using the bulk of the magnesium carbonate, silicon dioxide, and any unreacted rock/ore, the rock and/or gangue material from the first reaction phase is further processed to separate and remove specific valuable components therefrom. For example, elevated concentrations of certain precious metals (e.g., nickel, cobalt, chromium, and rare earth elements) in mafic and ultramafic rocks are further concentrated in this “slag” material. In at least one embodiment, highly elevated metal enrichments, that include but are not limited to phosphates, aluminum oxides, precious metals, and other mineral gangue may be separated from the remaining rock/ore by, for instance, heavy liquid separation or other gravity separation, or sluicing in a separator 418. Through gravity separation, the various metals and other valuable components are ground into fine particles and separated based on their individual specific weights.\|[0046] As illustrated in FIG. 4A, the first and second reactions can both occur in the same reactor 412, which may be a rotary kiln, fluidized bed, toroidal bed, or other reactor as described previously, in which case the reactions may be run sequentially, and all products separated at the completion of both reactions. In one or more embodiments (not shown in FIG. 4A), the reaction products (i.e., magnesium carbonate and silicon dioxide) may be separated after the first reaction step and prior to the second reaction step using established density separation techniques such as heavy liquid separation or other gravity separation, or sluicing. In other embodiments, as shown in FIG. 4A, the reaction products remain in the reactor during the second reaction step. Even if the reaction products are not physically separated, the thermochemical activity and reaction rates of fayalite and/or ferrosilite will increase according to the newly exposed surface area of fayalite and/or ferrosilite minerals. In other words, the reactivity of the serpentinization reactions with respect to the fayalite and/or ferrosilite minerals will proceed according to the now higher molar fraction of fayalite and/or ferrosilite in the solid solution (i.e., the number and/or extent of alternative side reactions has been reduced). With respect to the upper limit of the fully separated (e.g., using established density separation techniques such as heavy liquid separation or other gravity separation, or sluicing) or exposed fayalite and/or ferrosilite, the thermochemical activity of the powdered material should approach unity of the pure phase mineral, or mixtures of fayalite and/or ferrosilite mineral phases. Thus, the first reaction step involving the reaction of the forsterite with carbon dioxide increases the thermochemical driver for the second reaction step, which is the serpentinization/hydration reaction of the fayalite and/or ferrosilite with water, by reducing the availability of forsterite and increasing the exposed surface area of fayalite and/or ferrosilite minerals. The former increases the kinetic rate by driving the thermochemical activity toward that of a pure compound, while the latter enhances chemical activity by increasing the surface area available for reaction.\|[0047] FIG. 4B illustrates a flow diagram of another embodiment 400″ of a system of enhancing the production of hydrogen gas and magnetite from a source rock that contains a mixture including olivine (fayalite and forsterite) and/or pyroxene (ferrosilite and enstatite) minerals. The flow diagram of FIG. 4B is similar to that of FIG. 4A, except that the first reaction step occurs in a first reactor 412′ and the second reaction step occurs in a second reactor 412″. The first reactor 412′ facilities the carbonation reaction between the forsterite mineral and carbon dioxide. The crushed/ground ore of a uniform or pre-selected particle size range is passed from the sieve 408 or other particle size separator into the first reactor 412′. Carbon dioxide is pumped into the first reactor 412′ in above stoichiometric ratios to facilitate the carbonization reactions listed in Table 2. After the first reaction has occurred, the magnesium carbonate and silicon dioxide products, along with the unreacted fayalite and/or ferrosilite, and other remaining ore, are passed to the second reactor 412″.\|[0048] Continuing with FIG. 4B, the second reactor 412″ facilitates the serpentinization reaction between the fayalite and/or ferrosilite mineral phases and water (or steam). The reaction products and remaining rock/ore from the first reactor 412′ are introduced into the second reactor 412″. Water is pumped into the second reactor 412″ in above stoichiometric ratios (>˜20 liters/kg of rock) to facilitate the serpentinization reactions listed in Table 1. After the second reaction has occurred, the reactor gases, including the hydrogen gas evolved during the second reaction step, are passed or routed to a gas separator 414, as described above with respect to FIG. 4A. Likewise, the solid reaction products, including magnesium carbonate, silicon dioxide, magnetite, as well as any unreacted ore/rock are passed to a magnetic separator 416, as described above with respect to FIG. 4B. Other than the use of two reactors 412′ and 412″ in place of one reactor 412, as described above, the embodiments represented by FIGS. 4A and 4B are similar. It should be noted that the configuration of the system of FIG. 4B provides a semi-continuous method in that the separate process vessels, e.g., reactors 412′ and 412″, are dedicated to differing portions of the method.\|[0049] FIGS. 5, 6, and 7 illustrate flowcharts of various embodiments for enhancing the production of hydrogen gas, magnetite, magnesite, and scarce metal resources from mafic and ultramafic igneous rock that contains a mixture of olivine (fayalite and forsterite) and pyroxene (ferrosilite and enstatite) minerals. As previously disclosed in connection with FIG. 3, olivine- and/or pyroxene-rich ores may be found in numerous locations around the world. At block 502, such olivine- and/or pyroxene-rich ore may be acquired from geological sites containing high concentrations of such rocks in one or more of these areas. FIG. 6 illustrates this rock acquisition operation in greater detail. As shown at block 602, the olivine- and/or pyroxene-rich source rock may be acquired in any manner known to those skilled in the art, such as by underground mining, strip mining, quarrying, outcrop quarrying, or the use of waste (i.e., mine tailings), etc. The source rock may be transported, e.g., by barge, train, truck, etc., to a facility to further process the rock. In one or more embodiments, the source rock may be processed in proximity to the location where the rock is acquired. The source rock may be processed by crushing and/or grinding the rock at block 606 into smaller size fractions. In addition to creating uniform or near uniform sizing, such comminution also helps to expose the minerals, such as olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite), that are contained within the rock. If the rock is processed in proximity to the geological site from which the rock originated, then the processed rock may then be transported to a facility having a system to further extract hydrogen, magnetite, and other valuable products from the ore according to a method disclosed herein (not shown in FIGS. 5 and 6). At block 608, the crushed and/or ground source rock may be further processed by sieving or otherwise segregating the rock according to size. In one or more embodiments, the crushed and/or ground rock may be washed with water or a slightly acidic solution to clean the surfaces thereof of dust, dirt, or other contaminants. As illustrated at block 604, such washing may be conducted before the rock is crushed and/or ground and can also benefit from agitation.\|[0050] The crushed and/or ground rock is then introduced into a reactor at block 610 in which the rock is reacted with carbon dioxide and water to produce magnesium carbonate and hydrogen gas, among other products, in stoichiometric proportions via the carbonation reactions described in Table 2. The crushed/ground rock may be transported between and introduced into the reactor at block 610 by conveyor, by machinery placement, etc. A slightly acidic water solution, as previously described may be applied, e.g., by washing, spraying, or soaking, onto the outer surfaces of the rock. Such application may be before or after the rock is deposited in the reactor. The air in the reactor, including oxygen therein, may be evacuated from the sealed reactor with the rock disposed therein (e.g., by applying a vacuum to the reactor) or purged using reaction gas (e.g., N2) prior to commencing the reaction. Returning to FIG. 5, block 504 describes that carbon dioxide (CO2) is introduced into the reactor to begin the first reaction phase. The carbon dioxide may be gaseous or supercritical as previously described. A greater-than-stoichiometric portion of carbon dioxide is added as compared to the amount of rock (and specifically forsterite concentration therein) in the reactor in order to ensure that the carbon dioxide does not limit the carbonation reaction and to benefit from increased reactivity that is observed to occur at elevated pressures of CO2 and/or super-critical CO2. At block 504, the reactor is operated at one or more pre-selected temperatures and pressures, as described above, for a first residence time in order to sufficiently react the carbon dioxide with the forsterite mineral to produce magnesium carbonate and silicon dioxide reaction products. At the end of the first residence time, the gas phase from the reactor may be evacuated by, e.g., applying a vacuum or gas purging operation, to remove the excess unreacted carbon dioxide and any other gases evolved via the carbonation reactions of the first reaction phase.\|[0051] Continuing with FIG. 5, at block 506, water is introduced to the reactor after the first residence time. In one or more embodiments, the water is a low oxygen fugacity water that is prepared or obtained as described in greater detail above. Again, a greater-than-stoichiometric portion of water (>˜20 liters/kg of rock) is added as compared to the amount of rock (and specifically fayalite and/or ferrosilite concentrations therein) in the reactor in order to ensure that the water does not limit the serpentinization reaction. At block 506, the reactor is operated at one or more pre-selected temperatures and pressures, as described above, for a second residence time in order to sufficiently react the water with the fayalite and/or ferrosilite minerals (now having additional exposed surface area and more optimized chemical activity due to the first reaction phase) to produce at least hydrogen gas and magnetite reaction products.\|[0052] At block 508, the gas phase is removed from the reactor either during or at the completion of the second reaction phase. This gas phase, which is rich in hydrogen gas (and may contain small quantities of trace gases, e.g., N2, Ar, CO2) may be further purified through gas separator 414 (as shown in FIG. 4A and FIG. 4B). The gas separator 414 may be a pressure swing adsorption unit, a membrane separation unit, a cryogenic separation unit, or any other gas separation unit known to those skilled in the art. If the gas phase was not evacuated from the reactor between the first reaction phase and the second reaction phase, then some carbon dioxide and/or other gases, e.g., reaction gases, may contaminate the hydrogen gas evolved in the reactor via the serpentinization reactions of the second reaction phase.\|[0053] At block 510, the remaining rock within the reactor may be further processed to remove the magnesium carbonate/magnesite, the iron oxide/magnetite, the silicon dioxide, any remaining ore and/or slag material from the reactor. These operations are described in detail in connection with FIG. 7. Block 702 illustrates that the remaining rock in the reactor may be removed for further processing. Such removal may include removal by mechanical machinery, which picks up, rakes, or gravity feeds the material from the reactor into a container or onto a conveyor. In particular, at block 702 the solid reaction products (i.e., magnesite, magnetite, etc.), the remaining ore, and any slag material may be passed to a magnetic separator 416 (as shown in FIG. 4A and FIG. 4B) in order to separate the magnetite from the other materials via attraction of the magnetically susceptible iron oxide to a magnetic field (see block 704). The solid material removed from the reactor at block 702 may undergo additional crushing and/or grinding in order to create a fine powder to facilitate removal of valuable components thereof (not shown in FIGS. 5 and 7). At block 706, any precious or scarce metals that are now more concentrated in the remaining ore and/or gangue (collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) material after magnetite removal may be separated and removed based on density separation techniques such as heavy liquid separation or other gravity separation, or sluicing; an example of gravity separation using a gravity separator is shown in 480. Finally, as shown in block 708, the remaining rock, containing remaining magnesium carbonate (in which the carbon is permanently sequestered in the mineral phase), silicon dioxide, and any unreacted rock/ore may be used as an aggregate material and/or placed in landfill or otherwise disposed of. As noted previously, in some embodiments the magnesium carbonate and silicon dioxide may be separated (based on density separation techniques such as heavy liquids separation, or other gravity separation, or sluicing) and removed from the remaining rock/gangue (gangue: collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) materials for separate dispositioning.\|[0054] FIGS. 5, 6, and 7 illustrates operations performed in various example embodiments. It will be understood that each flowchart block, and each combination of flowchart blocks, may be implemented by various means. The flowchart blocks support combinations of means for performing the specified functions and combinations of operations for performing the specified functions. In some embodiments, some of the operations above may be modified or further amplified. Furthermore, in some embodiments, additional optional operations may be included. Modifications, amplifications, or additions to the operations above may be performed in any order and in any combination.\|(US12545576)\|Example Implementation\|[0055] In one example embodiment, an ultramafic ore was reacted with carbon dioxide to sequester the carbon in the magnesium carbonate mineral phase and water to evolve hydrogen gas as well as produce magnetite. The example was conducted in three phases: 1) rock preparation; 2) water preparation; and 3) reaction process, each of which will be described in greater detail below. As part of the analysis of the overall system and method, the composition of the ore (i.e., olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite) minerals), the reaction conditions to which the ore was subjected, and the characteristics of the carbonation/serpentinization reaction products were assessed. For instance, with respect to the ore composition, the mass, mineralogy, and geochemical composition of the bulk rock were evaluated by optical mineralogy, x-ray powder diffraction (XRD), and inductively coupled plasma mass spectrometry (ICP-MS) to evaluate the abundance of relevant constituents (e.g., fayalite, ferrosilite, FeO, MgO).\|[0056] In the rock preparation phase, an ultramafic aggregate material that included mostly rock particles of approximately 1 cm in size were collected from four active quarries (namely, two quarries in Pennsylvania, one in Virginia, and one in Kentucky). The ultramafic aggregate material was disaggregated (i.e., lightly crushed/comminuted) initially with a rock hammer and then with a Spex Ball mill. The powdered material was then sieved using grates arranged and designed to pass 150-, 80-, and then 45-micron grains successively. This enabled experimentation to be conducted on at least three different grains sizes. Another material—a homogenized olivine mineral—was also purchased from a scientific supplier in California. This olivine material, which was homogenized for size and composition, had a uniform particle size of approximately 100 microns.\|[0057] In the water preparation phase, three preparations were made. First, a low oxygen fugacity, high pH water was obtained by adding sodium bicarbonate and/or either sodium or potassium hydroxide to tap water in order to adjust the pH of the water to three levels 8.3, 9.7, and 11.1. As understood by those skilled in the art, oxygen fugacity (fO2) is a measure of the amount of oxygen available to react with elements having multiple valence states—such as iron and carbon. A high oxygen fugacity is indicative of a high chemical potential of oxygen in the water. A lowered oxygen fugacity of water can be achieved or in a variety of manners (e.g., by the use of low oxygen fugacity water supply such as municipal wastewater, groundwater, mine water, or other wastewater stream). One method for simply and reliably generating low oxygen fugacity water utilizes a heated bed of copper filings at 125° C. through which the water is passed to reduce the oxygen fugacity of the water (i.e., decrease the amount of reactive oxygen in the water). Such a method was used in this example implementation. Second, a saline water was obtained by adding salt (sodium chloride) to tap water to create saline solutions ranging from 0.1 to 4.5 per mil. In preparation for carbon mineralization experiments, the pH of the saline water was adjusted to be between about 4.8 and about 6.5 using dilute HCl in a mixture of distilled water and a sodium acetate buffer.\|[0058] For the reaction process, a single batch reactor (made of 316 stainless steel) was designed and built to conduct the carbonation and serpentinization reactions in both batch and sequential configurations. All of the reactions were performed in this closed stainless steel reaction vessel as a “batch” reaction (i.e., closed system) with the exception of a fluid sampling port that was opened periodically. For each experiment, whole samples (approximately 250 grams) were selected and sliced into two equally sliced approximately 125 grams of raw material and then placed in the gas-tight, stainless steel reaction vessels. In preparation for the introduction of carbon dioxide to the vessel, distilled water was lightly acidified using dilute hydrochloric acid and a sodium acetate buffer, and then mixed with salt (sodium chloride) to create a 0.1 to 4.5 per mil NaCl saline solution at ambient oxygen fugacity. This prepared water solution was then sprayed onto the powdered rock introduced into the reactor vessel. The prepared water solution provided a wet surface that enhanced the carbon dioxide reactivity with forsterite during the subsequent carbonation reactions.\|[0059] In the first reaction phase, sequestration of carbon dioxide was targeted through carbonation reactions between the introduced carbon dioxide and the forsterite (and enstatite) in the ore. The acidic, saline water, prepared as described above, was applied to the powdered rock containing the forsterite mineral prior to placing the wetted (i.e., sprayed with water solution as described above) powdered rock into the stainless-steel reaction vessel. Before the introduction of carbon dioxide, the reactor vessel was evacuated using a mechanical rough pump to apply a vacuum and remove air from the reactor vessel, including ambient oxygen. Other embodiments involve flushing the vessel with inert gas (e.g., N2) or reaction gas (e.g., CO2 or mixtures thereof) to remove air.\|[0060] Next, either carbon dioxide gas or mixtures of carbon dioxide gas, e.g., in a 4:1 ratio of carbon dioxide to nitrogen gas mixture, was introduced at room temperature and at an initial pressure of two bars (i.e., twice atmospheric pressure); in another embodiment of this disclosure, other ratios of CO2 to N2 can be utilized. The carbon dioxide used was an ultra-high purity carbon dioxide, such that the purity of carbon dioxide in the gas was greater than 99.9%, although mixtures with lower purity CO2 can be utilized in various embodiments. The temperature inside the reactor vessel was then increased to 100° C., 150° C., 200° C., 250° C., 300° C., and 400° C. with the temperature being controlled by an external band heater and measured with a standard Omega K-wire thermocouple. At each temperature, the gas phase pressure was measured via the sampling port using a standard Omega 0 to 100 psi pressure gauge. At each temperature, an aliquot of gas measured using a Stanford Research Systems residual gas analyzer (“quadrupole mass spectrometer”) and SRI gas chromatograph fitted with a thermocouple detector. The total pressure of hydrogen was calculated by determining the product of the percentage of hydrogen gas measured using the residual gas analyzer and/or gas chromatograph with the pressure compared to atmospheric pressure and assuming PV=nRT.\|[0061] The kinetic rate of carbon mineralization appeared to increase by ˜1.6 times when temperatures increased from 150° C. to 300° C., but additional increases in the rate of CO2 mineralization were not statistically significant between 300° C. and 400° C. over reaction times of ˜18 hours in the batch experiments. Next, while holding a constant temperature of 250° C., the pressure was increased to 5, 10, 25, and 50 bars of carbon dioxide. At each step, the gas phase pressure via the sampling port was monitored using a standard Omega 0 to 100 psi pressure gauge on an attached expansion volume (to ensure the sample pressure was in the range of the available pressure gauge). For each pressure, an aliquot of gas was also measured using an SRS quadrupole mass spectrometer and SRI gas chromatograph fitted with a thermocouple detector after pressure reduction by expansion to a pre-evacuated sample chamber via the sampling port. The rate of carbon mineralization appears to increase by ˜2.7 times between a pressure of 5 bars and 50 bars at 250° C.\|[0062] The preliminary results from the first reaction phase indicate that the kinetics of carbon dioxide mineralization increase with smaller grain sizes of the ore. There was a 23% improvement in the reduction of CO2 concentrations between 150 and 25 microns when holding temperature constant at 250° C., as determined based on CO2 pressure and concentration measurements and the mass of rock mineralized in the reaction vessel. While it is suspected that the removal of air will enhance the kinetics of carbon mineralization, at least one run without air/oxygen removal from the reactor vessel at the start of the first reaction phase did not appear to noticeably affect the carbonization reaction. Increasing both the temperature and the pressure of the reaction conditions increased the rate of CO2 mineralization up through at least 300° C. and 50 bars over reaction times of ˜18 hours in the batch experiments. Based on the plateau in the pressure of the reaction, these conditions are assumed to approach thermodynamic equilibrium in batch conditions between 12 and 18 hours, with variability observed throughout various experimental conditions (i.e., generally less time at higher temperature and pressure).\|[0063] During temperature increases from 100° C. to 300° C. at a constant pressure of 10 bars, the amount of mineralization increased from 14% additional mass (after 24 hours in a batch reactor) to 27%, representing a 92% increase in the mass of rock resulting from carbon mineralization. During pressure increases from 1 to 50 bar at a constant temperature of 250° C., the amount of mineralization increased from 4.1% additional mass (after 24 hours in a batch reactor) to 18.9%, representing a 4.6 times increase in the mass of rock resulting from carbon mineralization. Rotary kiln, fluidized bed, and toroidal bed processes were not evaluated in this process, but can be expected to substantially increase both the reaction rates and total efficiency of mineralization as compared to the batch process, even while temperature and pressure effects are expected to be similar to those in the batch process.\|[0064] In another experimental run, supercritical carbon dioxide was used in the reactor during the first reaction phase. Preliminary results indicate that the supercritical CO2 injected into the reactor at 10 bars and 250° C. reached a pressure plateau 4.5 hours (18.8%) faster than gaseous CO2. Thus, the carbon sequestration from this disclosed ex situ carbonation reaction may be maximized or enhanced while accounting for temperature and pressure in addition to other cost-intensive variables, such as energy input, material handling, and chemical processing costs. After the first reaction phase, the solid contents of the reactor were weighed. Based on a mass increase of between 39.3 grams (15.7%) at 150° C. at 5 bar and 101.6 grams (40.6%) at 300° C. at 50 bar, the abundance of total carbon mineralization was determined, which was verified using optical microscopy. Magnesite (i.e., magnesium carbonate), which was not observed in the initial experimental material, was identified, as expected based on the stoichiometry of the carbonation reaction resulting in a pre-concentration of an iron-rich iron-silica (fayalite and/or ferrosilite) phase prior to the second reaction phase.\|[0065] In the second reaction phase, liberation of the hydrogen was targeted through serpentinization/hydration reactions between the introduced water and the fayalite and/or ferrosilite (mixture in the four natural samples and exclusively olivine one prepared sample) in the remaining ore. Before the introduction of water with respect to the serpentinization reactions, the reactor vessel was evacuated using a mechanical rough pump to apply a vacuum and remove air from the reactor vessel including any remaining introduced carbon dioxide. Next, low oxygen fugacity (i.e., negative Eh value or negative electric potential), high pH (i.e., pH ranging between 8.3 and 11.1 using sodium bicarbonate or either sodium or potassium hydroxide), and saline (about 0.1 to 4.5 per mil sodium chloride (NaCl)) water, prepared as described above, was then introduced at room temperature and ambient atmospheric pressure into reactor vessel containing the remaining ore (i.e., unreacted ore consisting of the iron silicate phase, magnesium carbonate, silicon dioxide, residual olivine, pyroxene, and other accessory mineral phases).\|[0066] The initial gas phase pressure was measured/recorded via the sampling port using the standard Omega 0 to 100 psi pressure gauge. The temperature inside the reactor vessel was then increased to 50° C., 100° C., 150° C., 200° C., 250° C., 300° C., and 400° C. with the temperature being controlled by the external band heater and monitored with an Omega K-wire thermocouple. At each temperature step, the gas phase pressure was measured via the sampling port using the standard Omega 0 to 100 psi pressure gauge. At each temperature, an aliquot of gas was measured using a Stanford Research Systems residual gas analyzer (“quadrupole mass spectrometer”) and SRI gas chromatograph fitted with a thermocouple detector. The total pressure of hydrogen (and other gases) was calculated by determining the product of the percentage of hydrogen gas measured using the residual gas analyzer and/or gas chromatograph with the pressure compared to atmospheric pressure and assuming PV=nRT.\|[0067] The preliminary results from the second reaction phase indicated that the kinetics of hydrogen evolution increase with smaller grain sizes of the ore. There was a 5.2 times improvement in the yield of H2 between the temperature steps of 50° C. and 100° C. when holding a constant pressure of 10 bars as determined based on H2 partial pressure over a time interval of 18 hours. There was a 7.3 times improvement in the yield of H2 concentrations between the temperature steps of 100° C. and 400° C. when holding a constant pressure of 10 bars as determined based on H2 partial pressure over a time interval of 18 hours. The yield of H2 increased with pressure, but not to the same extent as temperature. There was a 31% times improvement in the yield of H2 between 1 and 5 bars at a constant temperature of 250° C., and a 1.8 times increase in the yield of H2 between 5 and 40 bars at a constant temperature of 250° C. as determined based on H2 partial pressure over a time interval of 18 hours. When compared to serpentinization reactions that were not preceded by the two-step carbonation reaction, the kinetic rates of the serpentinization reaction increase by 21% at 150° C. and up to 87% at 250° C. conducted at a constant pressure of 20 bars as compared to experiments performed at 100° C. This change is believed to be due to the carbonation-driven comminution of the ore that facilitated the initial breakdown of the rock/ore as well as the pre-concentration of the iron silicate mineral phases. The highest increase in the yield of H2 was 1.8 times above the yield observed at 100° C. and was observed at a temperature step of 200° C. following density separation of SiO2 and MgCO3 from the denser iron silicates by laboratory sluicing; this step yielded total H2 production of 0.576 mol H2/kg. Each increasing temperature step demonstrated an improvement in the purity of the hydrogen gas evolved; variable mixtures of N2, Ar and minor CO2 were observed in both the 50° C. and 100° C. temperature steps, which was less than 5% in the non-condensable fraction at temperatures above 150° C. with the exception of one sample at 400° C., which yielded 6.7% CO2.\|[0068] Along with the composition (%), the total pressure of the hydrogen gas that was formed by the reaction increased with higher temperatures, indicating a progressive increase in the kinetic rates and the total yield of hydrogen generation with higher temperature. Although this result was theoretically expected, it differentiates hydrogen produced by example embodiments described herein from hydrogen generated by natural systems wherein the occurrence of CO2, HCO3−, or other forms of carbon in the subsurface can begin to react with hydrogen at ˜150° C., which “short circuits” carbon-negative hydrogen generation by the formation of abiogenic methane via the Sabatier reaction (i.e., CO2+4H2→CH4+2H2O), wherein CO2 can be available as gaseous phase CO2 or be liberated from dissolved inorganic carbon phases in pore fluids by the following reaction: H++HCO3→CO2+H2O).\|[0069] A comparison of the disclosed two-step reaction was performed by further comparison to two base case single step reactions. The first base case comparison was a one-step reaction at a pH of 6.0 with temperatures increased from room temperature to 50° C., 100° C., 150° C., 200° C., 250° C., 300° C., and 400° C. The highest H2 yield at this pH was less than 0.011 mol H2/kg at 400° C., which was expected based on the mildly acidic conditions. The second base case comparison was a one-step reaction at a pH of 8.0 with temperatures increased from room temperature to 50° C., 100° C., 150° C., 200° C., 250° C., 300° C., and 400° C. At this pH and holding pressure constant at 20 bars, H2 yield in the single step reaction ranged from below detection limits at 50° C. at 18 hours to 0.051 mol H2/kg at 100° C. and up to 0.349 mol H2/kg at 400° C. For comparison, the highest value observed at the 400° C. in the single-step base case was 69.6% lower than the highest yield in the two-step reaction described above. Thus, the hydrogen gas production from this disclosed ex situ serpentinization reaction may be maximized or enhanced while accounting for temperature and pressure in addition to other cost-intensive variables, such as energy input, material handling, and chemical processing costs, especially by precluding interactions between H2 and labile carbon (i.e., CO2).\|[0070] After the sequential first and second reaction phases (i.e., the carbonation and serpentinization reactions) were completed in the reaction vessel, the mass (i.e., weight), mineralogy, and geochemical composition of the remaining bulk rock were determined by optical mineralogy and ICP-MS to evaluate the abundance (or lack) of relevant constituents (e.g., fayalite, ferrosilite, FeO, MgO, etc.). While visible olivine and pyroxene were still observed along with minor serpentine, the amount of magnetite observed was significantly higher (11-171% based on the mass of the separatable magnetic components) in the sequential reaction (i.e., first reaction phase followed by second reaction phase) than when the reaction was done without pre-concentration of the fayalite and/or ferrosilite minerals and control of reaction conditions, e.g., pH, low oxygen control, temperature. There was a 11% increase in the yield of magnetite between the temperature steps of 50° C. and 100° C. and approximately 13% between 100° C. and 150° C., while there was 1.7 times more magnetite recovered magnetically when comparing the 300° C. and 100° C. steps when holding a constant pressure of 10 bars over a time interval of 18 hours. Based on the stoichiometry of the reactions and these observations, it is apparent that an increased generation of magnetite is coupled with and inextricably linked to an increased generation of hydrogen (as was expected from the stoichiometric serpentinization reaction). These results support the stoichiometric modeling of both carbon dioxide mineralization (via carbonation) and hydrogen production (via serpentinization/hydration reactions). Thus, magnetite may be produced as a co-product of hydrogen generation/evolution (or vice versa based on the chosen business method).\|[0071] Additional analysis of the residual material identified highly elevated metal enrichments that included phosphates, aluminum oxides, and other poorly defined solids in the gangue (“mineral slag”). For example, lanthanum (one rare earth element) demonstrated an average concentration of 8.2 ppm in the bulk sample of ultramafic rock from the Pennsylvania quarry and 187.1 ppm in the residual gangue (largely aluminum oxide, phosphates and sulfides corresponding to roughly 2-4% of the total material). Similarly, nickel and cobalt concentrations were 133.9 and 78.2 ppm in a bulk sample of ultramafic rock from the same Pennsylvania quarry and 1,426 and 976.8 ppm in the residual gangue (largely aluminum oxide and sulfides). Separation of these metal enrichments may be accomplished by density separation techniques such as heavy liquid separation or other gravity separation, or sluicing or other methods known to those skilled in the art.\|[0072] The overall results indicate that, in the pursuit of carbon neutral or even negative carbon hydrogen production, the sequential carbonation and serpentinization reactions phases disclosed herein provide several reaction products (e.g., magnetite, rare earth elements, and other scarce metals) of economic and societal value in the pursuit of a lower carbon economy in addition to carbon sequestration and hydrogen evolution. Moreover, there exist a range of conditions where each reaction may be enhanced that varies only slightly with different rock contents, such that the reactions are more or less stable in the conditions described above among various sources of ultramafic and mafic rocks.\|[0073] As briefly discussed above, several reaction products have been identified from the staged, sequential carbonation and serpentinization reactions disclosed herein. Four reaction products in particular have the potential to be economically viable, especially when enhanced or enabled by steps, procedures, reaction conditions described herein that enhance the rock drivers comminution and thermodynamic toward idealized “carbonation” and serpentinization/hydration reactions. Adding to their economic viability, there may be revenue entitlements tied to the production of these reaction products, such as tax credits, sale of carbon credits, tax incentives, etc. The four products include: magnesite/aggregate, “green” or “golden” hydrogen (net carbon negative), magnetite, and scarce metals, and each will be discussed further hereinbelow.\|Magnesite\|[0074] The controlled ex situ generation of magnesite (magnesium carbonate) by enhancing “water-rock” serpentinization/hydration reactions involving mined, quarried, or waste (e.g., mine tailings) mafic or ultramafic rock and products provides an economic and carbon neutral (or even carbon negative) pathway for scalable magnesite and rock aggregate formation. This process can also economically increase the volume and mass of the rock (stoichiometric assessment of suitable mafic/ultramafic ores suggest the mass can increase by 34 to >60% (or 0.34 to >0.60 kg/kg of rock or 340 kg to >600 kg/metric ton of rock), while experimental results suggested at increase of 0.104 kg/kg (300° C. at 50 bars in the bulk rock obtained from the Pennsylvania quarry) to 0.237 kg/kg (300° C. at 50 bars in the pure olivine test sample). These values are expected to increase further by moving from a batch to dynamic reaction process (e.g., rotary kiln, fluidized bed, toroidal bed, or other similar processes) of rock compared to the original material introduced into the batch reactor.\|[0075] As disclosed, water having a pH of between about 4.8 to about 6.5 may be mixed with carbon dioxide in controlled conditions (e.g., under atmospheric or oxidizing conditions) to chemically break down the magnesium-rich silicate (i.e., forsterite) portion of mafic and ultramafic rocks. This reaction may be enhanced at temperatures of between about 150° C. to about 300° C. to 400° C. (although our experiment displayed a plateau in increased mineralization at 300° C.) and at pressures of at least up to 50 bars to produce magnesite. This carbonation process permanently sequesters carbon dioxide through the precipitation of magnesite mineral phases and other carbonate minerals, which can be used directly or as rock aggregate.\|[0076] The successful conversion of magnesium-silicate into magnesium carbonate and other carbonate minerals also allows the possibility to remove the bulk of the rock mass (following previously described density separation techniques) that can subsequently be either separated from residual iron-silicates or be separated prior to serpentinization/hydration reactions. The step of concentrating the iron silicate phase can further concentrate scarce metals (e.g., nickel, cobalt, rare earth elements) in other mineral forms (e.g., aluminum oxides, phosphates, and sulfides). This carbonation process is conducted first such that sequential serpentinization reactions may more readily and abundantly produce the reaction products of magnetite and hydrogen gas without the formation of accessory/competitive phases and enhance comminution.\|[0077] The importance of scalable and carbon negative (or carbon neutral) magnesium carbonate (magnesite) production has direct bearing on the numerous current uses of magnesite, including, but not limited to, pharmaceutical applications, agricultural lime and fertilizers (to neutralize acidification caused by fertilizer use), raw materials for ceramic and ceramic brick, and flux used in iron and steel manufacturing. Magnesite may also be used as a partial lime substitute to enable lower carbon emissions that result from the lower temperatures required to make magnesium oxide (MgO) as compared to calcium oxide (CaO). Further, magnesite can be used as a carbon negative concrete filler and cement or aggregate substitute in concrete.\|Green/Golden Hydrogen\|[0078] Hydration reactions involving iron-silicates (e.g., fayalite, ferrosilite) may be used to generate “green” (i.e., carbon neutral) or “golden” (i.e., carbon negative) hydrogen ex situ from mined, quarried, or waste streams of olivine- and/or pyroxene-rich ores, such as mafic and ultramafic rock. In one or more embodiments of the systems and method disclosed herein, the ex situ generation of carbon-negative hydrogen is directed to a two-reaction step/phase process in which: (1) carbon dioxide is first introduced in a gaseous or supercritical state into pulverized rock (approximately <150 microns) that has been wetted with a water preparation having a pH of between about 4.8 and about 6; and (2) water with a low oxygen fugacity (e.g., obtained from municipal wastewater, geothermal water, or other industrial water uses or made by reacting tap water over a bed of copper at 125° C.), a pH of between 8.3 and about 11.1 (the specified pH attained by adding sodium bicarbonate or either sodium or potassium hydroxide to the water but such water pH may be found in natural sources of water and wastewater) across a temperature range of between about 60° C. and about 400° C.\|[0079] The removal of a substantial portion of magnesium component from the powdered or comminuted rock in the first reaction phase increases the chemical (reaction) potential of the iron-rich portion in the second reaction phase. Stoichiometric calculations suggest that the chemical activity can be increased by up to eight times, while improvements of approaching a factor of two were observed in experiments; it is anticipated that the chemical activity and kinetics can be further increased by transitioning from a batch to dynamic process. Indeed, the rates of hydrogen production are significantly greater (nearly 70% greater) than in a method in which the iron-rich silicate mineral is reacted without the precursor step of carbon dioxide mineralization compared to a suitable base case for natural reactions or other one step engineered reaction processes.\|[0080] A significant advantage of various embodiments disclosed herein is that the systems and methods of such embodiments can be set up for ex situ operation almost anywhere in the world due to the vast and far-reaching reserves of mafic and ultramafic rock and availability of water and chemicals for amendment of pH and Eh of the water. Conversely, hydrogen formation in a more conventional manner, such as by natural gas reforming, is limited by natural gas availability, among other constraints that are often carbon intensive. Even if the produced carbon dioxide is sequestered, the hydrogen would be considered “blue,” not “green” or “golden.”\|Magnetite\|[0081] The controlled ex situ generation of magnetite by enhancing “water-rock serpentinization” reactions on mined, quarried, or waste streams of olivine- and/or pyroxene-rich ores and other materials provides an economic and carbon neutral (or even carbon negative) pathway for the production of magnetite while also enabling commensurate carbon dioxide sequestration through carbonate mineralization. While carbonation and serpentinization reactions are themselves naturally occurring, embodiments of the systems and methods disclosed herein are directed to enhanced magnetite production through the sequential ordering of these reactions in a controlled ex situ environment to limit alternative and undesirable chemical reactions capable of producing serpentine, brucite, or asbestos.\|[0082] In various embodiments disclosed herein, the ex situ generation of magnetite is directed to a two-reaction step/phase process in which: (1) carbon dioxide is first introduced in a gaseous or supercritical state in the presence of pulverized rock (approximately <150 microns) that has been wetted with a water preparation having a pH of between about 4.8 and about 6.5; and (2) water with a low oxygen fugacity (e.g., obtained from municipal wastewater, geothermal water, treated groundwater or other industrial water uses or made by reacting tap water over a bed of copper at 125° C.) having a pH of between 8.3 and about 11.1 (the specified pH attained by adding sodium bicarbonate or either sodium or potassium hydroxide to the water but such water pH may be found in natural sources of water and wastewater) is introduced across a temperature range of between about 80° C. and about 400° C. The two-step reaction at temperature >300° C. improves magnetite recovery by ˜1.7 times compared to lower temperatures and a suitable base case. Further, removal of a substantial portion of magnesium component from the powdered or comminuted rock in the first reaction step/phase increases the chemical (reaction) potential of the iron-rich portion in the second reaction step/phase (e.g., by approximately 23-800%), thereby increasing the thermodynamic drivers of magnetite generation several times. Thus, the generation of preferred mineral products, such as magnetite and hydrogen, is increased when compared to the random or undesired mineral species typically generated in natural systems. Indeed, the rates of magnetite production are significantly greater, and the targeted production of these specific chemical species is more reliable (e.g., the formation of serpentine, brucite, or asbestos are reduced) than in a method in which the iron-rich silicate mineral is reacted without the precursor step of carbon dioxide mineralization or in which both CO2 and water are reacted together (which occurs in natural systems).\|[0083] The Direct Reduction Iron (DRI) process is the only commercial low carbon emissions iron making process, and it is a precursor to steel manufacturing. The DRI process requires high-grade iron ore (greater than approximately 67% iron), which is in short supply in natural iron ores worldwide. Such limited access to magnetite (or other similarly iron-rich mineral phases) limits the potential to produce iron or steel using the DRI process, which is an important pathway for reducing carbon dioxide emissions in the steel industry. The systems and methods disclosed herein may produce high-grade iron ore (magnetite) in vast quantities due to the prolific occurrence of mafic and ultramafic rock, which accounts for greater than 10% of the continental crust and the vast majority of the oceanic crust. Moreover, the carbon dioxide sequestration tax credits and/or carbon credit sales associated with magnesite production may be attached to the magnetite output of these systems and methods. Thus, embodiments disclosed herein may increase the availability of high-grade iron ore to the steel industry along with a carbon credit, which may also result in the “greening” of the steel industry worldwide. Notably, the collective co-production (at one physical site) of magnesite, magnetite, and hydrogen gas also satisfies three requirements (i.e., iron-rich iron ore; reductive gas species/hydrogen; and magnesite flux) of iron making processes.\|Scarce Metals\|[0084] Elevated concentrations of certain relatively scarce metals (e.g., nickel, cobalt, chromium, and rare earth elements) in mafic and ultramafic rocks may be liberated and more easily recovered ex situ through sequential carbon sequestration/carbonation and “water-rock” serpentinization reactions involving mined, quarried, or waste mafic or ultramafic rock/ore. These scarce, and in some cases strategic, metals are critical for renewable energy and energy storage and are often derived from mining of weathered or processed minerals in more energy intensive steps (i.e., dehydration of asbestos back to forsterite). However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide. The reaction of gaseous or supercritical carbon dioxide with forsterite chemically breaks down these magnesium-rich silicate minerals and simultaneously sequesters carbon from carbon dioxide, while the reaction of water with fayalite and/or ferrosilite chemically breaks down the iron-rich silicate minerals and simultaneously produces magnetite and hydrogen gas. With the breakdown of these minerals, the remaining scarce metals are concentrated in the remaining unreacted ore and gangue (i.e., aluminosilicates, phosphates, accessory oxides, clay, etc.). Thus, the kinetic rates of the reactions of one or more embodiments disclosed herein and total metal recovery (i.e., higher concentrations in the starting composition) are much increased over natural chemical weathering of mafic and ultramafic rock. Further, the concentration of scarce metals is increased in the gangue, and the carbon footprint of “mining” or recovering these precious metals (and their derivative utilization in mobility and energy storage) is reduced. Therefore, the sequential carbonation and serpentinization reactions may provide for what is, in essence, a carbon negative mining of scarce and strategic metals.\|Conclusion\|[0085] Many modifications and other embodiments of the inventions set forth herein will come to mind to one skilled in the art to which these inventions pertain having the benefit of the teachings presented in the foregoing descriptions and the associated drawings. Therefore, it is to be understood that the inventions are not to be limited to the specific embodiments disclosed and that modifications and other embodiments are intended to be included within the scope of the appended claims. Moreover, although the foregoing descriptions and the associated drawings describe example embodiments in the context of certain example combinations of elements and/or functions, it should be appreciated that different combinations of elements and/or functions may be provided by alternative embodiments without departing from the scope of the appended claims. In this regard, for example, different combinations of elements and/or functions than those explicitly described above are also contemplated as may be set forth in some of the appended claims. Although specific terms are employed herein, they are used in a generic and descriptive sense only and not for purposes of limitation.	Family Number\|(104224295)\|104224295\|Object of Invention\|(WO202307466 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US20230102312 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US20230271827 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US12006212 B2)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(CA3227505 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(AU2022318480 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(IN202417013808 A)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US20240308843 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US12545576 B2)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|Advantages / Prev. Drawbacks\|(JP2024528907 A)\|The remaining rocks are advantageously deposited for the following section reaction steps by both of the grinding of the raw rock and the carbonation reaction occurring during the first reaction step, so that various combinations of grinding and the first reaction step can be used in various scenarios based on the desired result of a predetermined embodiment.\|	Environmental technology\|Materials, 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JP202020032422; US4798717; US20040087178; US20080299024; US20090308731; US20100313794; US20150152784; US20150157979; US20190131645; EP-236480; JP2020032422; JP2021513460; WO2013100333; WO2017222396; WO2019153047; WO2021138653; WO2023239797\|US20100313794; US20080299024; US20040087178; US20190131645; US4798717; US20190031645; US20150152784; US20090308731; US20150157979; WO2013100333; WO2021138653\|XP085850195; US20150157979; XP093030447; US20090308731; WO2013100333; WO2021138653\|\|US20150157979; US20090308731; WO2013100333; WO2021138653; XP085413764; WO2023239797; EP-236480; XP036373985\|US20150157979; JP2021513460; WO2017222396; JP2020032422\|\|\|\|	(EP4377258)\|Search Report references [Examiner]\|-KULARATNE KANCHANA ET AL: "Simultaneous ex-situ CO2mineral sequestration and hydrogen production from olivine-bearing mine tailings", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 95, 30 May 2018 (2018-05-30), pages 195 - 205, XP085413764, ISSN: 0883-2927, DOI: 10.1016/J.APGEOCHEM.2018.05.020\|-BASSEZ MARIE-PAULE ED - PIZZARELLO SANDRA: "Anoxic and Oxic Oxidation of Rocks Containing Fe(II)Mg-Silicates and Fe(II)-Monosulfides as Source of Fe(III)-Minerals and Hydrogen. Geobiotropy", ORIGINS OF LIFE AND EVOLUTION OF THE BIOSPHERE, KLUWER ACADEMIC PUBLISHERS, DORDRECHT, NL, vol. 47, no. 4, 31 March 2017 (2017-03-31), pages 453 - 480, XP036373985, ISSN: 0169-6149, [retrieved on 20170331], DOI: 10.1007/S11084-017-9534-5\|-See also references of WO 2023007466A1\|\|(US12545576)\|Examiner references\|-Kularatne et al. “Simultaneous ex-situ CO2 mineral sequestration and hydrogen production from olivine-bearing mine tailings.” Applied Geochemistry 95, p. 195-218 (2018).\|-Ehlmann, et al., “Ambient and cold-temperature infrared spectra and IRD patterns of ammoniated phyllosilcates and carbonaceous chondrite meteorites relevant to Ceres and other solar system bodies,” Meteorites Planetary Science, vol. 53, No. 9 (2018).\|-Wang, et al., “Pyroxene control H2 production and carbon storage during water-periodotite-CO2 hydrothermal reactions,” International Journal of Hydrogen Energy, vol. 44, p. 26835-26847; Sep. 11, 2019.\|-Bassez, Marie-Paule, “Anoxic and Oxic Oxidation of Rocks Containing Fe(II)Mg-Silicates and Fe(II)-Monosulfides as Source of Fe(III)-Minerals and Hydrogen. Geobiotropy”, Origins of Life and Evolution of the Biosphere, Kluwer Academic Publishers, vol. 47, No. 4, Mar. 31, 2017 (Mar. 31, 2017), pp. 453-480.\|\|(US12006212)\|Search Report references [Examiner]\|-Kularatne et al. "Simultaneous ex-situ CO2 mineral sequestration and hydrogen production from olivine-bearing mine tailings." APplied Geochemistry 95 (2018) 195-218 (Year: 2018)\|-Kularatne et al. “Simultaneous ex-situ CO2 mineral sequestration and hydrogen production from olivine-bearing mine tailings.” Applied Geochemistry 95 (2018) 195-218 (Year: 2018).\|-Ehlmann, et al., Ambient and cold-temperature infrared spectra and IRD patterns of ammoniated phyllosilcates and carbonaceous chondrite meteorites relevant to Ceres and other solar system bodies, Meteorites & Planetary Science, vol. 53, No. 9, 2018 [retrieved on Oct. 5, 2022]. Retrieved from the internet, <URL:https://onlinelibrary.wiley.com/dol/pdf/10.1111/maps.13103>, pp. 1884-1901.\|-Wang, et al., Pyroxene control H2 production and carbon storage during water-peridotite-CO2 hydrothermal reactions, International Journal of Hydrogen Energy, vol. 44, Sep. 11, 2019, pp. 26835-26847.\|\|\|(WO2023/007466)\|International Search Report [Examiner]\|-WANG ET AL.: "Pyroxene control of H2 production and carbon storage during water-peridotite-CO2 hydrothermal reactions", INTERNATIONAL JOURNAL OF HYDROGEN ENERGY, vol. 44, 11 September 2019 (2019-09-11), pages 26835 - 26847, XP085850195, DOI: 10.1016/j.ijhydene.2019.08.161\|-EHLMANN BETHANY L., ROBERT HODYSS, THOMAS F. BRISTOW, GEORGE R. ROSSMAN, ELEONORA AMMANNITO, M. CRISTINA DE SANCTIS, CAROL A. RAYM: "Ambient and cold-temperature infrared spectra and XRD patterns of ammoniated phyllosilicates and carbonaceous chondrite meteorites relevant to Ceres and other solar system bodies", METEORITICS & PLANETARY SCIENCE, vol. 53, no. 9, 23 April 2018 (2018-04-23), pages 1884 - 1901, XP093030447, DOI: 10.1111/maps.13103\|-See also references of EP 4377258A4\|\|\|\|\|\|	GRANTED	(EP4377258)\|PENDING\|(US12545576)\|GRANTED\|(US12006212)\|GRANTED\|(US20230102312)\|LAPSED\|(WO2023/007466)\|LAPSED\|(JP2024528907)\|REVOKED\|(BR112024001825)\|PENDING\|(IN202417013808)\|PENDING\|(AU2022318480)\|PENDING\|(CA3227505)\|PENDING	ALIVE	(EP4377258)\|ALIVE\|(US12545576)\|ALIVE\|(US12006212)\|ALIVE\|(US20230102312)\|DEAD\|(WO2023/007466)\|DEAD\|(JP2024528907)\|DEAD\|(BR112024001825)\|ALIVE\|(IN202417013808)\|ALIVE\|(AU2022318480)\|ALIVE\|(CA3227505)\|ALIVE	(EP4377258)\|LEGAL DETAILS FOR EP4377258\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-07-29\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP22848809\|Application date=2022-07-29\|Standardized application number=2022EP-0848809\|Event publication date=2023-02-03\|Event code=EP/STAAPCT\|Event group=Examination events Entry into national phase\|The international publication has been made\|Original code: STAA\|Event publication date=2024-05-03\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2024-05-03\|Event code=EP/STAARQ\|Event indicator=Pos\|Event group=Examination events\|Request for examination was made\|Original code: STAA\|Event publication date=2024-06-05\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP4377258\|Publication stage code=A1\|Publication date=2024-06-05\|Standardized publication number=EP4377258\|Event publication date=2024-06-05\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2024-02-20\|Event publication date=2024-06-05\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2024-11-06\|Event code=EP/DAV\|Event indicator=Neg\|Event group=Designated states\|Request for validation of the European patent (deleted)\|Request for validation of the european patent (in any country) deleted\|Event publication date=2024-11-06\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2025-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP4377258\|Publication stage code=A4\|Publication date=2025-09-17\|Standardized publication number=EP4377258\|Event publication date=2025-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2025-08-19\|Event publication date=2025-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2025-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication 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code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1735\|Event publication date=2023-04-18\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 2890822.00005\|Event publication date=2023-04-18\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 178846\|Event publication date=2023-04-18\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2023-04-18\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2023-04-18\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2023-04-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2023-04-18\|Event code=US/ENT\|Event group=Administrative 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OAO\|Restriction/Election Requirement\|Event publication date=2023-08-31\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20230271827\|Publication stage code=A1\|Publication date=2023-08-31\|Standardized publication number=US20230271827\|Event publication date=2023-08-31\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2023-09-12\|Event code=US/ELC\|Event group=Examination events OAI\|Response to Election / Restriction Filed\|Event publication date=2023-10-07\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2023-10-12\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2023-10-12\|R4R=112b\|RJST=non-final\|Rejected claims 17\|Event publication date=2023-10-12\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2023-10-12\|R4R=102a\|RJST=non-final\|Rejected claims 8, 13, 14\|RJCT=US20100313794\|Event publication date=2023-10-12\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2023-10-12\|R4R=103\|RJST=non-final\|Rejected claims 1, 8, 13-15; 2, 3; 4; 5, 11; 7, 9-10, 16; 9-10, 16; 17\|RJCT=US20080299024\|RJCT=US20040087178\|RJCT=US20190131645\|RJCT=US20100313794\|RJCT=US4798717\|RJCT=US20190031645\|Event publication date=2024-01-12\|Event code=US/INVSUM\|Event group=Examination events OAI INT\|Interview Summary- Applicant Initiated\|Event publication date=2024-01-16\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2024-02-05\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2024-02-07\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2024-05-07\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DARRAH, THOMAS;RAO, VIKRAM;WHYTE, COLIN\|Reel/frame:067334/0570\|OWNER:OHIO STATE INNOVATION FOUNDATION, OHIO\|Effective date of the event=2021-07-30\|Event publication date=2024-05-07\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2024-05-07\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2024-05-09\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2024-05-22\|Event code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=2024-05-22\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2024-06-11\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US12006212\|Publication stage code=B2\|Publication date=2024-06-11\|Standardized publication number=US12006212\|Event publication date=2024-06-11\|Event code=US/MEPGNTF\|Event group=Event indicating In Force Administrative notifications\|Mail Patent eGrant Notification\|Event publication date=2024-06-11\|Event code=US/EPGNTF\|Event group=Event indicating In Force Administrative notifications\|Patent eGrant Notification\|Event publication date=2024-06-11\|Event code=US/EPG\|Event group=Event indicating In Force\|Recordation of Patent eGrant\|Event publication date=2024-06-11\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=0\|(US20230102312)\|LEGAL DETAILS FOR US20230102312\|Actual or expected expiration date=2023-06-09\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-07-28\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US17815914\|Application date=2022-07-28\|Standardized application number=2022US-17815914\|Event publication date=2022-07-28\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:HOUSE, KIMBERLY ANN\|Event publication date=2022-07-28\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 178846\|Event publication date=2022-07-28\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2022-07-28\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=3974\|Event publication date=2022-07-28\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 2890822.00002\|Event publication date=2022-07-28\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2022-07-28\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2022-07-28\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2022-07-28\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DARRAH, THOMAS;RAO, VIKRAM;WHYTE, COLIN\|Reel/frame:060664/0083\|OWNER:OHIO STATE INNOVATION FOUNDATION, OHIO\|Effective date of the event=2021-07-30\|Event publication date=2022-08-08\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2022-08-10\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2022-12-09\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2022-12-09\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2022-12-23\|Event code=US/PTDI\|Event group=OAO\|Petition Decision - Dismissed\|Event publication date=2022-12-23\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2023-01-09\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-01-30\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2023-03-30\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20230102312\|Publication stage code=A1\|Publication date=2023-03-30\|Standardized publication number=US20230102312\|Event publication date=2023-03-30\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2023-06-09\|Event code=US/ABNEA\|Event indicator=Neg\|Event group=Event indicating Not In Force OAI\|Expressly Abandoned -- During Examination\|Event publication date=2023-06-09\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-06-09\|Event code=US/ODPD6\|Event group=Administrative notifications\|GRANTED - Express Abandonment Petition Decision under 37 CFR 1.138 (d)\|(WO2023/007466)\|LEGAL DETAILS FOR WO2023/007466\|Actual or expected expiration date=2025-01-30\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-07-29\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOIB2022/057088\|Application date=2022-07-29\|Standardized application number=2022WO-IB57088\|Event publication date=2023-02-02\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2023/007466\|Publication stage code=A1\|Publication date=2023-02-02\|Standardized publication number=WO202307466\|Event publication date=2025-01-30\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2022318480\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2022318480\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2022AU-0318480\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2022318480\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2024-02-22\|Publication number in the designated or member state=AU2022318480\|Event publication date=2024-02-07\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2024-02-22\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=AU\|MEMBER STATE LEGAL DETAILS FOR BR112024001825\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=BR Corresponding appl: BR112024001825\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2024BR-0001825\|Corresponding cc:\|Designated or member state=BR Corresponding pat: BR112024001825\|Publication stage code in the designated or member state=A0\|Publication date in the designated or member state=2024-02-06\|Publication number in the designated or member state=BR112024001825\|Event publication date=2024-02-06\|Event code=WO/REG\|Event code=BR/B01A\|Event group=Examination events\|Reference to a national code\|Pct publication - request for entry into the national phase\|Comunicacao da publicacao internacional pct. apresentacao de peticao de requerimento de entrada na fase nacional\|Corresponding cc:\|Designated or member state=BR\|Event publication date=2024-04-24\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2024-01-29\|Corresponding cc:\|Designated or member state=BR\|MEMBER STATE LEGAL DETAILS FOR CA3227505\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA3227505\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2022CA-3227505\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA3227505\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2023-02-02\|Publication number in the designated or member state=CA3227505\|Event publication date=2024-01-30\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2024-03-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2024-03-01\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP4377258\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP22848809\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2022EP-0848809\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP4377258\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2024-06-05\|Publication number in the designated or member state=EP4377258\|Event publication date=2023-03-15\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2024-02-29\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2024-03-03\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2024-02-29\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR IN202417013808\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN202417013808\|Application date in the designated or member state=2024-02-26\|Application number in the designated or member state=2024IN-17013808\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN202417013808\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2024-03-15\|Publication number in the designated or member state=IN202417013808\|Event publication date=2024-02-26\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|MEMBER STATE LEGAL DETAILS FOR JP2024528907\|Actual or expected expiration date=2026-03-09\|Legal state=DEAD\|Status=REVOKED\|Corresponding cc:\|Designated or member state=JP Corresponding appl: JP2024505303\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2024JP-0505303\|Corresponding cc:\|Designated or member state=JP Corresponding pat: JP2024528907\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2024-08-01\|Publication number in the designated or member state=JP2024528907\|Event publication date=2024-01-29\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=JP\|(JP2024528907)\|LEGAL DETAILS FOR JP2024528907\|Actual or expected expiration date=2026-03-09\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2022-07-29\|Event code=JP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=JP JP2024505303\|Application date=2022-07-29\|Standardized application number=2024JP-0505303\|Event publication date=2024-05-21\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2024-03-22\|Event publication date=2024-05-21\|Event code=JP/A621\|Event indicator=Pos\|Event group=Examination events\|Written request for application examination\|Japanese intermediate code: A621\|Effective date of the event=2024-03-22\|Event publication date=2024-08-01\|Event code=JP/A\|Event group=Examination events\|Published application\|Publication country=JP\|Publication number=JP2024528907\|Publication stage code=A\|Publication date=2024-08-01\|Standardized publication number=JP2024528907\|Event publication date=2025-03-19\|Event code=JP/A977\|Event group=Examination events\|Report on retrieval\|Japanese intermediate code: A971007\|Effective date of the event=2025-03-19\|Event publication date=2025-04-15\|Event code=JP/A131\|Event indicator=Neg\|Event group=Examination events\|Notification of reasons for refusal\|Japanese intermediate code: A131\|Effective date of the event=2025-04-15\|Event publication date=2025-07-14\|Event code=JP/A601\|Event group=Examination events\|Written request for extension of term\|Japanese intermediate code: A601\|Effective date of the event=2025-07-14\|Event publication date=2025-08-04\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2025-08-04\|Event publication date=2025-08-19\|Event code=JP/A131\|Event indicator=Neg\|Event group=Examination events\|Notification of reasons for refusal\|Japanese intermediate code: A131\|Effective date of the event=2025-08-19\|Event publication date=2025-11-18\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2025-11-18\|Event publication date=2025-12-09\|Event code=JP/A02\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Decision of refusal\|Japanese intermediate code: A02\|Effective date of the event=2025-12-09\|Event publication date=2025-12-09\|Event code=JP/RF121\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Article 121 of the Patent Act, Expected Rejection Date\|Effective date of the event=2026-03-09\|Event publication date=2026-04-08\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2026-04-08\|(BR112024001825)\|LEGAL DETAILS FOR BR112024001825\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-07-29\|Event code=BR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=BR BR112024001825\|Application date=2022-07-29\|Standardized application number=2024BR-0001825\|Event publication date=2024-02-06\|Event code=BR/A0\|Event indicator=Pos\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=BR\|Publication number=BR112024001825\|Publication stage code=A0\|Publication date=2024-02-06\|Standardized publication number=BR112024001825\|Event publication date=2024-04-24\|Event code=BR/A2\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention / pipeline patent published without search report\|Publication country=BR\|Publication number=BR112024001825\|Publication stage code=A2\|Publication date=2024-04-24\|Standardized publication number=BR112024001825\|(IN202417013808)\|LEGAL DETAILS FOR IN202417013808\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-02-26\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN202417013808\|Application date=2024-02-26\|Standardized application number=2024IN-17013808\|Event publication date=2024-03-15\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN202417013808\|Publication stage code=A\|Publication date=2024-03-15\|Standardized publication number=IN202417013808\|(AU2022318480)\|LEGAL DETAILS FOR AU2022318480\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-07-29\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2022318480\|Application date=2022-07-29\|Standardized application number=2022AU-0318480\|Event publication date=2024-02-22\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2022318480\|Publication stage code=A1\|Publication date=2024-02-22\|Standardized publication number=AU2022318480\|(CA3227505)\|LEGAL DETAILS FOR CA3227505\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-07-29\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA3227505\|Application date=2022-07-29\|Standardized application number=2022CA-3227505\|Event publication date=2023-02-02\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA3227505\|Publication stage code=A1\|Publication date=2023-02-02\|Standardized publication number=CA3227505\|Event publication date=2024-02-02\|Event code=CA/EEER\|Event indicator=Pos\|Event group=Examination events\|Examination request\|Effective date of the event=2024-01-30\|Event publication date=2024-07-19\|Event code=CA/MFA\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|MAINTENANCE FEE FOR APPLICATION PAID\|Annual fees payment date=2024-07-19\|Year of payment of annual fees=2\|Fee description text: MF (APPLICATION, 2ND ANNIV.) - SMALL\|Event publication date=2024-07-19\|Event code=CA/U00\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FEE PAID\|ST27 STATUS EVENT CODE: A-2-2-U10-U00-U101 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE REQUEST RECEIVED\|Effective date of the event=2024-07-19\|Event publication date=2024-07-19\|Event code=CA/U11\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FULL RENEWAL OR MAINTENANCE FEE PAID\|ST27 STATUS EVENT CODE: A-2-2-U10-U11-U102 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE FEE PAYMENT PAID IN FULL\|Effective date of the event=2024-07-19\|Event publication date=2025-07-25\|Event code=CA/MFA\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|MAINTENANCE FEE FOR APPLICATION PAID\|Annual fees payment date=2025-07-25\|Year of payment of annual fees=3\|Fee description text: MF (APPLICATION, 3RD ANNIV.) - SMALL\|Event publication date=2025-07-25\|Event code=CA/U00\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FEE PAID\|ST27 STATUS EVENT CODE: A-2-2-U10-U00-U101 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE REQUEST RECEIVED\|Effective date of the event=2025-07-25\|Event publication date=2025-07-25\|Event code=CA/U11\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FULL RENEWAL OR MAINTENANCE FEE PAID\|ST27 STATUS EVENT CODE: A-2-2-U10-U11-U102 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE FEE PAYMENT PAID IN FULL\|Effective date of the event=2025-07-25\|Event publication date=2025-10-27\|Event code=CA/D15\|Event group=Examination events\|EXAMINATION REPORT COMPLETED\|ST27 STATUS EVENT CODE: A-2-2-D10-D15-D126 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: EXAMINER'S REPORT\|Effective date of the event=2025-10-27\|Event publication date=2026-02-25\|Event code=CA/P11\|Event group=Corrections Examination events\|AMENDMENT OF APPLICATION REQUESTED\|ST27 STATUS EVENT CODE: A-2-2-P10-P11-P100 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: AMENDMENT RECEIVED - RESPONSE TO EXAMINER'S REQUISITION\|Effective date of the event=2026-02-25\|Event publication date=2026-02-26\|Event code=CA/P11\|Event group=Corrections Examination events\|AMENDMENT OF APPLICATION REQUESTED\|ST27 STATUS EVENT CODE: A-2-2-P10-P11-P102 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: AMENDMENT DETERMINED COMPLIANT\|Effective date of the event=2026-02-26\|Event publication date=2026-02-26\|Event code=CA/P13\|Event group=Corrections\|APPLICATION AMENDED\|ST27 STATUS EVENT CODE: A-2-2-P10-P13-X000 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: APPLICATION AMENDED\|Effective date of the event=2026-02-26\|Event publication date=2026-02-26\|Event code=CA/W00\|Event group=Administrative notifications\|OTHER EVENT OCCURRED\|ST27 STATUS EVENT CODE: A-2-2-W10-W00-W111 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: CORRESPONDENT DETERMINED COMPLIANT\|Effective date of the event=2026-02-26	(EP4377258)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2023/007466)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2023/007466)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2023/007466)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2023/007466)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2023/007466)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP4377258)\|EP; DE\|(US12545576)\|US\|(US12006212)\|US\|(WO2023/007466)\|AU; BR; CA; EP; IN\|(BR112024001825)\|BR\|(IN202417013808)\|IN\|(AU2022318480)\|AU\|(CA3227505)\|CA	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=8TP/cX+h8x4s9VnBCZbBPnmXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023293142&ekey=1944&xpn=EP4377258&kind=A4	https://register.epo.org/application?number=EP22848809	https://permalink.orbit.com/RenderStaticFirstPage?XPN=aIV65hZo%252BWIbWDK85JFymXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(US12545576)\|US\|(US20240308843)\|US\|(US12006212)\|US\|(US20230271827)\|US\|(WO2023/007466)\|US\|(US20230102312)\|US	(US12545576)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US , ATYP=US State Government\|(US20240308843)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US\|(US12006212)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US , ATYP=US Company\|(US20230271827)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US\|(WO2023/007466)\|NAME=OHIO STATE INNOVATION FOUNDATION 1524 North High Street Columbus, Ohio 43201 , COUNTRY=US\|(US20230102312)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US	(EP4377258)\|DE\|\|\|(WO2023/007466)\|US\|\|(AU2022318480)\|AU\|(CA3227505)\|CA	(EP4377258)\|NAME=K&L Gates LLP;Karolinen Karree Karlstraße 12 , CITY=80333 München , COUNTRY=DE , REG=101744768\|(US12545576)\|NAME=K&L Gates LLP\|(US12006212)\|NAME=K&L Gates LLP\|(WO2023/007466)\|NAME=EASWARAN, David Womble Bond Dickinson (US) LLP Attn: Patent Docketing P.O. Box 570489 Atlanta, Georgia 30357 , POSTCODE=30357 , COUNTRY=US\|(JP2024528907)\|NAME=KIMURA, Mitsuru , REG=100095407NAME=Yasushi Morikawa , REG=100132883NAME=Kei Sakurada , REG=100148633NAME=Hide Mie , REG=100147924\|(AU2022318480)\|NAME=K&L Gates Level 25 South Tower 525 Collins Street , CITY=Melbourne , STATE=VIC , POSTCODE=3000 , COUNTRY=AU\|(CA3227505)\|NAME=ROWAND LLP , COUNTRY=CA	\|(EP4377258)\|US; US; US\|(US12545576)\|US; US; US\|(US20240308843)\|US; US; US\|(US12006212)\|US; US; US\|(US20230271827)\|US; US; US\|(US20230102312)\|US; US; US\|(WO2023/007466)\|US; US; US\|\|\|\|\|(CA3227505)\|US; US; US	(EP4377258)\|NAME=DARRAH, Thomas\|NAME=RAO, Vikram\|NAME=WHYTE, Colin\|(EP4377258)\|NAME=DARRAH, Thomas, CITY=Columbus, Ohio 43210, COUNTRY=US \|NAME=RAO, Vikram, CITY=Columbus, Ohio 43210, COUNTRY=US \|NAME=WHYTE, Colin, CITY=Columbus, Ohio 43210, COUNTRY=US\|(US12545576)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(US20240308843)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(US12006212)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(US20230271827)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(US20230102312)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(WO2023/007466)\|NAME=DARRAH, Thomas c/o 1524 North High Street Columbus, Ohio 43210, POSTCODE=43210, COUNTRY=US \|NAME=RAO, Vikram c/o 1524 North High Street Columbus, Ohio 43210, POSTCODE=43210, COUNTRY=US \|NAME=WHYTE, Colin c/o 1524 North High Street Columbus, Ohio 43210, POSTCODE=43210, COUNTRY=US\|(JP2024528907)\|NAME=THOMAS DARRAH\|NAME=Rao, Bikram\|NAME=COLIN WHYTE\|(BR112024001825)\|NAME=DARRAH THOMAS\|NAME=RAO VIKRAM\|NAME=WHYTE COLIN\|(IN202417013808)\|NAME=Darrah Thomas\|NAME=Rao Vikram\|NAME=Whyte Colin\|(AU2022318480)\|NAME=DARRAH, Thomas\|NAME=RAO, Vikram\|NAME=WHYTE, Colin\|(CA3227505)\|NAME=DARRAH, THOMAS, COUNTRY=US \|NAME=RAO, VIKRAM, COUNTRY=US \|NAME=WHYTE, COLIN, COUNTRY=US	(US12545576)\|7\|(US12006212)\|7\|(WO2023/007466)\|7\|(IN202417013808)\|7\|(JP2024528907)\|7\|(AU2022318480)\|7\|(CA3227505)\|7\|(US20230102312)\|7	5	10			(EP4377258)\|WO2023/007466\|(JP2024528907)\|WO2023/007466\|(BR112024001825)\|WO2023/007466\|(IN202417013808)\|WO2023/007466\|(AU2022318480)\|WO2023/007466\|(CA3227505)\|WO2023/007466		(US12545576)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=11\|Independent Claim Number: ICL=1,18\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Term Disclaimers Indicated TDI=Term Disclaimers Indicated\|Extended under 35 USC 154(b) the following days: EXTD=0\|Primary examiner: Wartalowicz Paul A\|Art Unit.: ART =1735\|\|(US20240308843)\|Number of Claims: NCL=19\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,17\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: Wartalowicz Paul A\|Art Unit.: ART =1735\|\|(US12006212)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=11\|Independent Claim Number: ICL=1,10,20\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=0\|Primary examiner: Wartalowicz Paul A\|Art Unit.: ART =1735\|\|(US20230271827)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,8,18\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|Primary examiner: Wartalowicz Paul A\|Art Unit.: ART =1735\|\|(US20230102312)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,8,18\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|\|(WO2023/007466)\|Number of Claims: NCL=67\|Extended kind: EXTK=x\|\|(JP2024528907)\|Number of Claims: NCL=67\|Request for examination: REQEXA=true\|\|(IN202417013808)\|Number of Claims: NCL=67\|\|(AU2022318480)\|Number of Claims: NCL=67\|\|(CA3227505)\|Number of Claims: NCL=20\|	(US12545576)\|Continuation of: US18/302,702 FDD=2023-04-18 [2023US-18302702]\|Continuation of: US17/815,914 FDD=2022-07-28 [2022US-17815914]\|Continuation of: US12006212 \|Provisional Appl: US63/203,814 FDD=2021-07-30 [2021US-63203814]\|Previous publication: US20240308843 A1 2024-09-19 [US20240308843]\|(US12006212)\|Continuation of: US17/815,914 FDD=2022-07-28 [2022US-17815914]\|Provisional Appl: US63/203,814 FDD=2021-07-30 [2021US-63203814]\|Previous publication: US20230271827 A1 2023-08-31 [US20230271827]\|(US20230102312)\|Provisional Appl: US63/203,814 FDD=2021-07-30 [2021US-63203814]	(EP4377258)\|ENGLISH (ENG)	(US12545576)\|Patent\|(EP4377258)\|Patent\|(US20240308843)\|Patent\|(JP2024528907)\|Patent\|(US12006212)\|Patent\|(EP4377258)\|Patent\|(BR112024001825)\|Patent\|(IN202417013808)\|Patent\|(AU2022318480)\|Patent\|(BR112024001825)\|Patent\|(US20230271827)\|Patent\|(US20230102312)\|Patent\|(CA3227505)\|Patent\|(WO202307466)\|Patent	Titre: (EP4377258)\|Systems and methods for generating hydrogen and magnetite from rock Résumé: (EP4377258)\|Systems and methods for sequestering carbon, evolving hydrogen gas, producing iron oxide as magnetite, and producing magnesium carbonate as magnesite through sequential carbonation and serpentinization/hydration reactions involving processed olivine- and/or pyroxene-rich ores, as typically found in mafic and ultramafic igneous rock. Precious or scarce metals, such nickel, cobalt, chromium, rare earth elements, and others, may be concentrated in the remaining ore to facilitate their recovery from any gangue material.	43	Abstract	gpt-4o-mini	yes	The patent describes methods for sequestering carbon through carbonation reactions involving olivine, which aligns with the topic of enhanced weathering and carbon capture.
44	JP2021075533	JP2021075533	JP7699796\|JP2022169854	102507569	JP7699796 B2 2025-06-30 [JP7699796]\|JP2022169854 A 2022-11-10 [JP2022169854]	2021-04-28	2021-04-28	2025-06-30\|2022-11-10	(JP7699796)\|2025-06-30	(JP7699796)\|2041-04-28	(JP7699796)\|How to remove carbon dioxide from the air	(JP7699796)\|PROBLEM TO BE SOLVED: To provide a method which can be executed at low cost, can substantially reduce carbon dioxide, and removes carbon dioxide in the air friendly to an environment with no risk of storing the carbon dioxide.SOLUTION: The present invention atomizes a rock containing an alkaline earth metal, immobilizes carbon dioxide to the rock by bringing acquired fine particles into contact with the air in a space as prescribed environment to mineralize carbon dioxide in the air as carbonate, and removes the carbon dioxide in the air. The invention can easily remove the carbon dioxide in the air at low cost without using chemical, and can remove qualitative carbon dioxide with little production amount of accompanying carbon dioxide. In addition, the immobilized carbon dioxide becomes carbonate harmless to environment and friendly to the environment with no risk of storing the carbon dioxide.SELECTED DRAWING: Figure 1COPYRIGHT: (C)2023,JPO&INPIT	WASEDA UNIVERSITY	(JP7699796)\|WASEDA UNIVERSITY\|(JP2022169854)\|WASEDA UNIVERSITY	COREY ADAM MYERS\|NAKAGAKI TAKAO	(JP7699796)\|Myers, Corey Adam\|NAKAGAKI Takao\|(JP2022169854)\|COREY ADAM MYERS\|NAKAGAKI TAKAO	(JP7699796)\|HATA, Masanori\|Reg. Nb: 100115842	(JP7699796)\|It is desirable that at least 5000 (or 10000) particles are analyzed for each sample of the compound.\|Table 3 confirms that the present invention works more advantageously than other technologies.\|The present invention can be advantageously used as a means for providing a technique that enables carbon dioxide in the air to be immobilized as a carbonate on a rock to reduce carbon dioxide in the air, and has high industrial applicability.\|Furthermore, the method disclosed in the non-patent document 3 is a method for simply dispersing crushed rocks on the soil surface, which is undesirable because it is difficult to estimate the amount of carbon dioxide mineralization and may adversely affect the environment.\|On the other hand, such a method does not reduce greenhouse gases because it has a large energy load and a large amount of carbon dioxide emissions.\|These transport and storage systems are too large and costly for individual companies to manufacture and operate, and there are various political, economic, and social risks associated with achieving CDR. dependent on systems that store carbon dioxide underground.\|	(JP7699796)\|1. A method for removing carbon dioxide from the air, wherein a compound (excluding a carbonate) containing at least one of Ca (calcium) and Mg (magnesium) is used. of rock to obtain fine particles of the rock; and The method includes a carbonate formation step in which the fine particles of the rock thus obtained are brought into contact with air in a space having a temperature of 15-50°C and a relative humidity of 50-100%, and carbonates are formed in the fine particles of the rock The amorphous portion of the rock is 30 mass% or less of the whole, and the fine particles of the rock have a particle diameter of 1-100 μm The fine particles of the rock are put in the tray in a state of spreading in a laminar state over the entire bottom surface of the tray, and are brought into contact with the air by placing the tray in the space A method for removing carbon dioxide from the air, characterized in that the fine particles of the rock spread in the layer have a thickness of 1 to 50 mm.\|	(JP7699796)\|An aspect of the present invention is explained below.\|The present invention provides an environmentally friendly method for removing carbon dioxide from the air, the method being implemented at a low cost, being capable of substantially reducing carbon dioxide, and being free from the risk of carbon dioxide retention.\|The present invention relates to a method for removing carbon dioxide from air. More specifically disclosed is a method for removing carbon dioxide from the air, which enables the conversion of carbon dioxide from the air into a useful and harmless state by mineralizing carbon dioxide as a carbonate.\|	(JP7699796)\|CARBON DIOXIDE(100,117)\|AIR(100,53)\|ROCK FINE PARTICLE(100,22)\|REMOVING CARBON DIOXIDE(100,14)\|DISPERSING CRUSHED ROCK(75,1)\|ROCK(54,71)\|ULTRABASIC ROCK(49,3)\|FINE PARTICLE(44,39)\|TRAY(43,13)\|CARBON DIOXIDE CONVERSION(36,1)\|CARBON DIOXIDE MINERALIZATION(35,7)\|WASTE CONCRETE(35,6)\|CARBONATE FORMATION(32,6)\|ENVIRONMENTALLY FRIENDLY(32,4)\|CARBON DIOXIDE RETENTION(30,2)\|SOCIAL RISK(30,1)\|CARBON DIOXIDE EMISSION(27,4)\|PGM TAILING MINERAL CARBONATION(27,1)\|REDUCING CARBON DIOXIDE(27,1)\|GRAVEL(26,3)\|GREENHOUSE GAS(25,1)\|CALCIUM ALUMINATE(24,9)\|PARTICLE DIAMETER(24,5)\|GROUND SURFACE(20,1)\|ROCK AMORPHIZATION(19,2)\|MINERALIZATION RATE(18,9)\|WORLD OCEAN ACIDIFICATION(18,1)\|ROCK PARTICLE(17,4)\|SLAG MINERALIZATION RATIO(17,2)\|BIBIORNITHOSPHERITE ORNITHOSPHERITE(17,1)\|MONOLITHOSPHERITE ORNITHOSPHERITE(17,1)\|MAGNESIUM OXIDE(15,19)\|SLAG RAPID MINERALIZATION(15,1)\|MAGNESIUM ALUMINOSILICATE(14,2)\|PULSATILE ROCK(14,2)\|NATURAL ROCK(13,15)\|ENTIRE BOTTOM(13,3)\|FAST MINERALIZATION REACTION(13,2)\|BASALT IC ROCK(13,1)\|CALCIUM FERROUS ALUMINATE(13,1)\|DANG ORNITHOSPHERITE(13,1)\|MACHINERY INDUSTRIALIZATION(13,1)\|MICROPARTICULATING ROCK(13,1)\|NATURAL SUPRABASIC ROCK(13,1)\|SUPRAPACEOUS ROCK(13,1)\|IRON OXIDE(12,12)\|CRYSTALLINE MINERAL(12,2)\|DEEP ROCK(12,2)\|FINE STONE PARTICLE(12,2)\|MINERALIZATION POTENTIAL(12,2)\|CO2 MINERALIZATION(12,1)\|MICRONIZING ROCK(12,1)\|ROCK MINERALIZATION PERFORMANCE(12,1)\|ROCK PARTICULATE(12,1)\|ULTRAPASCULAR STONE(12,1)\|WHOLE ROCK REACTIVITY(12,1)\|RELATIVE HUMIDITY(11,7)\|CAAL2SI2O(11,5)\|CAMGSIO(11,5)\|CALCIUM SILICATE IRON(11,3)\|ROCK COMPONENT(11,3)\|UNREACTED NUCLEAR MODEL(11,3)\|CA2SIO(10,4)\|ATOMIZED ROCK(10,1)\|ATOMIZING ROCK(10,1)\|BIOMASS COMBUSTION(10,1)\|CALCIUM FERROALUMINATE(10,1)\|EARTH CLIMATE(10,1)\|ENVIRONMENTALLY HARMLESS CARBONATE(10,1)\|LARGE ENERGY LOAD(10,1)\|MIXED CATION SILICATE(10,1)\|MOTTLED ROCK(10,1)\|NUCLEATION CRYSTAL DISTRIBUTION(10,1)\|ROCK FINE PARTICLE AMORPHIZATION(10,1)\|SILICATED MINERAL(10,1)\|ULTRAFINE ROCK(10,1)\|MORTAR(9,5)\|COMPOUND REACTION(9,2)\|MINERALIZE CARBON DIOXIDE(9,2)\|PARTICULATE SAMPLE(9,2)\|SIO CONTENT(9,2)\|CA2AL2SIO(8,3)\|CA2FE2O(8,3)\|CA2MGSI2O(8,3)\|CA3MGSI2O(8,3)\|CA3SI2O(8,3)\|CA3SIO(8,3)\|CA7MGSI4O(8,3)\|CALCIUM ALUMINOSILICATE(8,3)\|CAMGSI2O(8,3)\|IGNEOUS ROCK(8,3)\|ALKALINE MINERAL(8,1)\|ALUMINA SILICATE(8,1)\|CALCIUM SILICATE MAGNESIUM MOIETY(8,1)\|CO2 DIFFUSION(8,1)\|COMPOUND GRINDING(8,1)\|CRUSHER LOAD(8,1)\|INCUBATOR INDOOR SPACE(8,1)\|IRON SUBSTITUTION(8,1)\|MAGNESIUM ALUMINA OXIDE(8,1)\|MINERALIZATION DECREASE(8,1)\|ORE MATRIX(8,1)\|SLAG PARTICLE(8,1)\|USABLE ROCK(8,1)\|SEA(7,3)\|AMORPHOUS DIAMETER(7,2)\|CA3AL2O(7,2)\|CRYSTALLINE LAYER(7,2)\|IMMOBILIZED CARBON DIOXIDE(7,2)\|MAGNESIUM ALUMINATE(7,2)\|MGFE2O(7,2)\|OLIVINE(7,2)\|ROCK CRUSHING(7,2)\|SCRAPER(7,2)\|TRANSPORTATION(7,2)\|ALKALINE EARTH METAL(6,16)\|CARBON DIOXIDE REMOVAL(6,4)\|MANGANESE OXIDE(6,4)\|DACCS(6,3)\|ALKALI MINERAL(6,1)\|AMORPHIZATION DIAMETER(6,1)\|AMORPHOUS PHASE ACCOUNT(6,1)\|CALCIUM IRON ALUMINATE(6,1)\|CALCIUM IRON SILICATE(6,1)\|CALCIUM MAGNESIUM SILICATE(6,1)\|CALCIUM SILICATE MAGNESIUM SILICATE(6,1)\|CIRCULAR TRAY(6,1)\|CIVILIZATION(6,1)\|CO2 REDUCTION(6,1)\|CRYSTALLINE COMPOUND(6,1)\|ELAPSED DAY(6,1)\|FUTURE CO2(6,1)\|GROUND SLAG(6,1)\|IRON MOIETY(6,1)\|IRON SLAG(6,1)\|MAGNESIUM ION(6,1)\|MAJOR CHALLENGE(6,1)\|MICROPARTICLE FORMATION(6,1)\|MT SCALE(6,1)\|POTENTIAL CARBON FOOTPRINT ASSESSMENT(6,1)\|SAMPLE PARTICLE(6,1)\|STEEL SLAG(6,1)\|STORAGE SYSTEM(6,1)\|STUDY TREATMENT START(6,1)\|VOLUME INCUBATOR(6,1)\|BECCS(5,3)\|CASIO(5,3)\|OPTICAL MICROSCOPE(5,3)\|PRODUCT LAYER(5,3)\|ACCOUNTING(5,1)\|AIR CO2(5,1)\|AIR RECOVERY(5,1)\|ATOMIZATION(5,1)\|BERYLLIUM(5,1)\|BIOENERGY(5,1)\|CA CONTENT(5,1)\|CA12AL14O(5,1)\|CA3AL2SI(5,1)\|CA3FE2SI3O(5,1)\|CAFESI2O(5,1)\|CALCIUM MAGNESIUM IRON SILICATE(5,1)\|CALCIUM OXIDE MINERALIZATION RATIO(5,1)\|CARBON DIOXIDE CAPTURE(5,1)\|CARBON DIOXIDE DIFFUSION(5,1)\|CARBON DIOXIDE OXIDATION(5,1)\|CARBON DIOXIDE SHOW MINERALIZATION(5,1)\|CLASSIFICATION FUNCTION(5,1)\|CLIMATE CHANGE REPORT(5,1)\|CO2 SEQUESTRATION(5,1)\|COMPOUND DIFFUSION COEFFICIENT(5,1)\|CREATION(5,1)\|CRUSHED ROCK FINE PARTICLE(5,1)\|DEEP REGION(5,1)\|DISLOCATION(5,1)\|EXCEPTION(5,1)\|EXHAUST FUME REMOVAL(5,1)\|FACTORY(5,1)\|FE2SIO(5,1)\|FINE PARTICLE CLASSIFICATION(5,1)\|GENERATED CARBONATE(5,1)\|GLOBAL CARBON DIOXIDE(5,1)\|HUMIDITY CONDITION(5,1)\|IMAGEJ(5,1)\|IMPLEMENTATION PERIOD(5,1)\|INORGANIC COMPONENT(5,1)\|IRON ION(5,1)\|KG SCALE(5,1)\|KOMATIITE(5,1)\|LANDFILL(5,1)\|MAFIC ROCK(5,1)\|MARINE ECOSYSTEM(5,1)\|METAMORPHIC ROCK(5,1)\|MG3AL2SI(5,1)\|MICROMETER LEVEL(5,1)\|MINERALIZATION REACTION DEGREE(5,1)\|MOLAR DENSITY(5,1)\|MULTISTAGE(5,1)\|NET CARBON DIOXIDE(5,1)\|NET REDUCTION(5,1)\|PARTICLE PROCESSING(5,1)\|PARTICULATE LAYER(5,1)\|PETERSEN(5,1)\|PHOTOSYNTHESIS(5,1)\|POROSITY(5,1)\|\|(JP2022169854)\|AIR(100,63)\|REMOVING CARBON DIOXIDE(100,21)\|DISPERSING CRUSHED ROCK(93,1)\|ROCK FINE PARTICLE(92,19)\|PULVERIZED ROCK(82,4)\|ROCK(68,72)\|BRINGING FINE PARTICLE(67,1)\|CARBON DIOXIDE(57,121)\|MINERALIZATION(47,25)\|CARBONATE FORMATION(46,3)\|IMMOBILIZED CARBON DIOXIDE(46,1)\|FINE PARTICLE(45,49)\|CARBON DIOXIDE MINERALIZATION(45,8)\|WASTE CONCRETE(45,8)\|FINE PARTICLE ACQUISITION(44,1)\|QUALITATIVE CARBON DIOXIDE(44,1)\|GRAVEL(42,1)\|MINERALIZE CARBON DIOXIDE(37,4)\|PGM TAILING MINERAL CARBONATION(33,1)\|GREENHOUSE GAS(31,1)\|CALCIUM ALUMINATE(29,9)\|MINERAL(26,4)\|AMORPHOUS PHASE(25,13)\|GROUND SURFACE(25,1)\|CARBON DIOXIDE REDUCTION(24,6)\|CARBON DIOXIDE REMOVAL(24,5)\|VAPOR PHASE CARBON DIOXIDE(23,1)\|WORLD OCEAN ACIDIFICATION(23,1)\|CO2 MINERALIZATION(21,2)\|DEEPENING ROCK(21,2)\|ULTRABASAL ROCK(21,2)\|ATMOSPHERIC PRESSURE(19,1)\|ENERGY LOAD(19,1)\|MONOORTHORITE PERIDOTITE(19,1)\|ALKALINE EARTH METAL(18,19)\|MINERALIZATION RATE(18,5)\|MAGNESIUM ALUMINOSILICATE(18,2)\|PULVERIZED ROCK FINE PARTICLE(18,2)\|AMORPHOUS COMPOUND(16,4)\|FAST MINERALIZATION REACTION(16,2)\|VAPOR PHASE(16,2)\|DIPLOITE PERIDOTITE(16,1)\|MACHINERY INDUSTRIALIZATION(16,1)\|NATURAL SUPERBASIC ROCK(16,1)\|ROCK AMORPHIZATION(16,1)\|ROCK MICROPARTICLE(16,1)\|ULTRABASTITE ROCK(16,1)\|NATURAL ROCK(15,13)\|CALCIUM IRON OXIDE(15,6)\|CALCIUM SILICATE MAGNESIUM(15,3)\|CRYSTALLINE MINERAL(15,2)\|MINERALIZATION POTENTIAL(15,2)\|CAMGSI2O(14,5)\|CAMGSIO(14,5)\|GANGUE(14,5)\|MORTAR(14,5)\|CALCIUM IRON ALUMINATE(14,3)\|ELAPSED DAY(14,3)\|IRON CALCIUM SILICATE(14,3)\|SIO CONTENT(14,3)\|ADVANCING MINERALIZATION REACTION(14,1)\|HARMLESS CARBONATE(14,1)\|ORE HOST ROCK(14,1)\|ROCK MINERALIZATION PERFORMANCE(14,1)\|SLAG MINERALIZATION RATIO(14,1)\|ULTRAMAGNETIC ROCK(14,1)\|WHOLE ROCK REACTIVITY(14,1)\|RELATIVE HUMIDITY(13,7)\|ROCK COMPONENT(13,3)\|CA2SIO(12,4)\|CAAL2SI2O(12,4)\|ENVIRONMENTALLY FRIENDLY(12,4)\|LARGE SCALE EQUIPMENT(12,2)\|MICROPARTICULATION(12,2)\|PARTICLE DISTRIBUTION(12,2)\|ROCK WHOLE(12,2)\|UNREACTED NUCLEAR MODEL(12,2)\|ARTIFICIAL STONE(12,1)\|ATOMIZING ROCK(12,1)\|BIOMASS COMBUSTION(12,1)\|EARTH CLIMATE(12,1)\|EXCESS CONCRETE(12,1)\|FINE STONE PARTICLE(12,1)\|PATCHY ROCK(12,1)\|RAPID MINERALIZATION(12,1)\|CA2AL2SIO(11,3)\|CA2FE2O(11,3)\|CA3MGSI2O(11,3)\|CA3SI2O(11,3)\|CA3SIO(11,3)\|CA7MGSI4O(11,3)\|CALCIUM ALUMINOSILICATE(11,3)\|CARBON DIOXIDE EMISSION(11,3)\|GUIDELINE(11,3)\|IGNEOUS ROCK(11,3)\|OLIVINE(11,3)\|ALKALI ORE(10,1)\|ALKALINE MINERAL(10,1)\|ALUMINA SILICATE(10,1)\|COMPOUND GRINDING(10,1)\|INCUBATOR INDOOR SPACE(10,1)\|LAYERED ROCK FINE PARTICLE(10,1)\|MICROPARTICLE SAMPLE(10,1)\|MINERALIZATION DECREASE(10,1)\|PULVERIZER LOAD(10,1)\|ROCK PARTICLE(10,1)\|SLAG PARTICLE(10,1)\|ATOMIZATION(9,2)\|CA2MGSI2O(9,2)\|CA3AL2O(9,2)\|CARBON DIOXIDE DIFFUSION(9,2)\|MAGNESIUM ALUMINATE(9,2)\|MGFE2O(9,2)\|OLECITE(9,2)\|PESTLE(9,2)\|PHYLITE(9,2)\|STORAGE RISK(9,2)\|FINE PARTICLE SAMPLE(8,4)\|MANGANESE OXIDE(8,4)\|AMORPHIZED(8,1)\|CALCIUM IRON SILICATE(8,1)\|CIRCULAR TRAY(8,1)\|CIVILIZATION(8,1)\|CO2 DIFFUSION COEFFICIENT(8,1)\|CO2 REMOVAL(8,1)\|COMPOUND REACTION(8,1)\|CRYSTALLINE COMPOUND(8,1)\|DECREASING PARTICLE(8,1)\|FINE PARTICLE PERFECT DISTRIBUTION(8,1)\|GROUND SLAG(8,1)\|IMAGEJ(8,1)\|IRON MAGNESIUM SILICATE(8,1)\|MAGNESIUM ION(8,1)\|MAGNESIUM IRON SILICATE(8,1)\|MAJOR CHALLENGE(8,1)\|MT SCALE(8,1)\|PARTICULATE SAMPLE(8,1)\|POTENTIAL CARBON FOOTPRINT ASSESSMENT(8,1)\|PROMOTION(8,1)\|PULVERIZATION LAYER(8,1)\|PULVERIZED COMPOUND PARTICLE DIAMETER(8,1)\|STEEL SLAG(8,1)\|TERMINATION TREATMENT(8,1)\|ULTRABASITE(8,1)\|UNREACTED NUCLEUS MODEL(8,1)\|PARTICLE SIZE(7,12)\|BECCS(7,3)\|DACCS(7,3)\|OPTICAL MICROSCOPE(7,3)\|PRODUCT LAYER(7,3)\|CDR(7,2)\|AIR RECOVERY(6,1)\|AL2SI3O(6,1)\|ALUMINA MAGNESIUM OXIDE(6,1)\|AMORPHOUS CHANGE(6,1)\|AMORPHOUS DIAMETER(6,1)\|ARBITRARY AREA TRAY(6,1)\|ATMOSPHERIC CARBON DIOXIDE(6,1)\|AVAILABLE ROCK(6,1)\|BASALITE(6,1)\|BERYLLIUM(6,1)\|CA CONTENT(6,1)\|CA3FE2SI3O(6,1)\|CAFESI2O(6,1)\|CAFESIO(6,1)\|CALCIUM OXIDE MINERALIZATION RATIO(6,1)\|CARBON DIOXIDE RECOVERY(6,1)\|CARBON DIOXIDE RETENTION(6,1)\|CLASSIFICATION FUNCTION(6,1)\|CLIMATE CHANGE REPORT(6,1)\|CO2 SEQUESTRATION(6,1)\|CRUSHING(6,1)\|DANORITE(6,1)\|DISARRANGEMENT(6,1)\|DOLERITE(6,1)\|EMITTED CARBON DIOXIDE(6,1)\|EXCEPTION(6,1)\|FACTORY(6,1)\|FE2SIO(6,1)\|GENERATED CARBONATE(6,1)\|GLOBAL CARBON DIOXIDE(6,1)\|GLOBAL ENVIRONMENT PROTECTION(6,1)\|GROUP REACTION(6,1)\|IMPLEMENTATION MENSTRUATION(6,1)\|INORGANIC COMPONENT(6,1)\|IRON CALCIUM MAGNESIUM SILICATE(6,1)\|IRON ION(6,1)\|KG SCALE(6,1)\|KOMACHIITE(6,1)\|LANDFILL(6,1)\|MAFIC ROCK(6,1)\|	(JP7699796)\|1. A method for removing carbon dioxide from the air, wherein a compound (excluding a carbonate) containing at least one of Ca (calcium) and Mg (magnesium) is used. of rock to obtain fine particles of the rock; and The method includes a carbonate formation step in which the fine particles of the rock thus obtained are brought into contact with air in a space having a temperature of 15-50°C and a relative humidity of 50-100%, and carbonates are formed in the fine particles of the rock The amorphous portion of the rock is 30 mass% or less of the whole, and the fine particles of the rock have a particle diameter of 1-100 μm The fine particles of the rock are put in the tray in a state of spreading in a laminar state over the entire bottom surface of the tray, and are brought into contact with the air by placing the tray in the space A method for removing carbon dioxide from the air, characterized in that the fine particles of the rock spread in the layer have a thickness of 1 to 50 mm.\|2. The method for removing carbon dioxide in the air described in claim 1 is characterized in that the rock contains at least one kind of compound selected from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|3. The method for removing carbon dioxide in the air described in Claim 1 or Claim 2 is characterized in that the rock contains at least one compound in the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate in an amount of at least 5 mass% of the total amount of the rock.\|4. The method for removing carbon dioxide in the air described in any of claims 1 to 3 is characterized in that the rock contains at least one kind of ultra-basic rock, basic rock, slag and waste concrete.	(JP7699796)\|TECHNICAL FIELD\|[0001] The present invention relates to a method for removing carbon dioxide from air. More specifically disclosed is a method for removing carbon dioxide from the air, which enables the conversion of carbon dioxide from the air into a useful and harmless state by mineralizing carbon dioxide as a carbonate.\|BACKGROUND ART\|[0002] It is obvious that carbon dioxide emitted into the atmosphere is the cause of global warming, which has been a problem in recent years. Reducing such carbon dioxide emissions is a major challenge in protecting the global environment.\|[0003] Carbon dioxide is naturally captured from the atmosphere through biological processes such as photosynthesis by plant life on land and in the ocean, but the concentration of carbon dioxide in the atmosphere continues to rise. Carbon dioxide is also said to be a factor in the acidification of the world's oceans, which poses a threat to marine ecosystems. On the other hand, systems for fixing and removing exhaust fumes from factories and carbon dioxide (CO2) gas in the atmosphere have been proposed in various ways (for example, see Patent Document 1, etc.). ).\|[0004] Net reduction of global carbon dioxide (CO2) concentrations to eliminate or reduce atmospheric CO2 is It is referred to as NET (Negative Emission Technology) or Carbon Dioxide Removal (CDR.) and various technologies are available (see, for example, Non-Patent Document 1 or Non-Patent Document 3). ).\|[0005] The carbon dioxide emitted must be removed from the atmosphere to stabilize the Earth's climate within a range compatible with modern civilization. Also, in general, the techniques described in the literature described above should be applied to biological systems (e.g., retention of carbon dioxide in soil, plants, or the ocean). ) or highly industrialized machinery that filters carbon dioxide from the air, liquefies it, and stores it underground. And, there was a tendency that chemicals, high temperature and special reactor were required for industrial process which depended on such machinery.\|CITATION LIST\|PATENT LITERATURE\|[0006] Special Report No. 2013-504424\|NON PATENT LITERATURE\|[0007] Nduagu, E., Bergerson, J. and Zevenhoven, R., 2012. Life cycle assessment of CO2 sequestration in magnesium silicate rock A comparative study. Energy Conversion and Management, 55, pp.116-126.\|Ncongwane, M.s., Broadhurst, J.L. and Petersen, J., 2018. Assessment of the potential carbon footprint of engineered processes fwor the mineral carbonation of PGM tailings. International Journal of Greenhouse Gas Control, 77, pp.70-81.\|Keller, d.P., Lenton, A., Littleton, E.w., Oschlies, A., Scott, v. and Vaughan, N.E., 2018. The effects of carbon dioxide removal on the carbon cycle. Current climate change reports, 4(3), pp.250-265.\|DISCLOSURE\|TECHNICAL PROBLEM\|[0008] Carbon dioxide mineralization in rocks occurs naturally over hundreds of thousands of years. However, conventional methods to promote the reaction are high temperature and high pressure, or by adding chemicals. On the other hand, such a method does not reduce greenhouse gases because it has a large energy load and a large amount of carbon dioxide emissions.\|[0009] Concretely, the technology disclosed in the non-patent document 1 has a problem that the substantial reduction in carbon dioxide amount is reduced because carbon dioxide is reacted with carbon dioxide under high temperature and high pressure conditions. In addition, the technology disclosed in Non-Patent Document 2 requires the addition of chemicals and background emissions during its production (e.g., carbon dioxide emissions related to the creation, transportation, termination and disposal of chemicals and additives). As with the technology disclosed in Non-Patent Document 1, substantial CO2 reductions were reduced by the use of CO2-P-P (Carbon Dioxide Reduction Method).\|[0010] Furthermore, the method disclosed in the non-patent document 3 is a method for simply dispersing crushed rocks on the soil surface, which is undesirable because it is difficult to estimate the amount of carbon dioxide mineralization and may adversely affect the environment.\|[0011] The direct removal of carbon dioxide from the atmosphere is only a part of the total amount of carbon dioxide removal (CDR.) that has already been released, which is in line with the climate change reduction target. The removed carbon dioxide must be transported to the appropriate location for disposal and stored deep underground in certain geological structures. These transport and storage systems are too large and costly for individual companies to manufacture and operate, and there are various political, economic, and social risks associated with achieving CDR. dependent on systems that store carbon dioxide underground.\|[0012] The present invention provides an environmentally friendly method for removing carbon dioxide from the air, the method being implemented at a low cost, being capable of substantially reducing carbon dioxide, and being free from the risk of carbon dioxide retention.\|TECHNICAL SOLUTION\|[0013] The method for removing carbon dioxide from the air according to the present invention is a method for removing carbon dioxide from the air, wherein a compound (excluding a carbonate) contains at least one of Ca (calcium) and Mg (magnesium). of rock to obtain fine particles of the rock; and The method includes a carbonate formation step in which the fine particles of the rock thus obtained are brought into contact with air in a space having a temperature of 15-50°C and a relative humidity of 50-100%, and carbonates are formed in the fine particles of the rock The amorphous portion of the rock is 30 mass% or less of the whole, and the fine particles of the rock have a particle diameter of 1-100 μm The fine particles of the rock are put in the tray in a state of spreading in a laminar state over the entire bottom surface of the tray. The rock is characterized in that the rock particles which are brought into contact with the air by placing the tray in the space and spread in the layer form have a thickness of 1 to 50 mm.\|[0014] The method for removing carbon dioxide from the air is characterized in that the rock contains at least one compound from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|[0015] The method for removing carbon dioxide from the air is characterized in that the rock contains, in a total amount, 5 mass% or more of at least one compound from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|[0017] The method for removing carbon dioxide from the air is characterized in that the rock contains at least one member selected from among ultra-basic rock, basic rock, slag and waste concrete.\|ADVANTAGEOUS EFFECTS\|[0020] The present invention secures carbon dioxide to a rock and removes carbon dioxide from the air by atomizing the rock containing an alkaline earth metal, bringing the obtained particulates into contact with air in a space having a predetermined environment, and mineralizing carbon dioxide in the air as a carbonate.\|[0021] Consequently, the present invention can easily remove carbon dioxide from the air at low cost without using a chemical or using a large-scale facility, etc., and can substantially reduce carbon dioxide because the amount of carbon dioxide generated is small. In addition, there is no need of storing carbon dioxide, and there is no risk in such storage, and the immobilized carbon dioxide becomes a carbonate harmless to the environment, and can be reused together with rocks, so that it is also environmentally friendly.\|DESCRIPTION OF DRAWINGS\|[0022] This chart (Graph 1) shows the change in the mineralization effect (mineralization rate (%)) of carbon dioxide in the atmosphere as a result of measuring the number of elapsed days as 14 days.\| This chart (Graph 2) shows the change in the mineralization effect (mineralization rate (%)) of carbon dioxide in the atmosphere as the number of months in December (one year).\|DESCRIPTION OF EMBODIMENTS\|[0023] An aspect of the present invention is explained below. The method for removing carbon dioxide from the air according to the present invention comprises atomizing a rock containing an alkaline earth metal ((I) atomization step) and bringing the atomized rock into contact with the air in a space having a specific environment Carbon dioxide in the air is mineralized and fixed by using carbon dioxide in the air as a carbonate ((II) carbonate formation process) to remove the carbon dioxide from the air.\|[0024] Step (A): In the step of atomizing, the rock is pulverized to obtain fine particles.\|[0025] (A-1) About rocks: First, I will explain available rocks. Any of natural and man-made rocks can be used as rocks if they are formed from the compounds, etc. shown below. In the present invention, the term "compound" also includes "mineral".\|[0026] Usable rocks are, for example, 0-100°C temperature, suitable moisture (for example, relative humidity of reaction environment is 50-100%, etc.). It is required that the formation of carbonate by reaction with gas phase carbon dioxide under atmospheric pressure is thermodynamically possible. The term "thermodynamically" is taken to mean that 0-dimensional calculation conditions are considered and meso-scale structures are not considered.\|[0027] The rocks usable in the present invention are so-called slags (steel slags, iron slag, etc.), which are composed of a substance containing a mineral component of an ore matrix, etc., which has been separated by melting from a metal to be metallurgically measured, when smelting the metal from the ore, etc., as rocks containing a compound containing an alkaline earth metal. In addition, concrete that was originally used for buildings, etc., such as demolished concrete that is created when the building itself is no longer necessary or when the building, etc. that used the building, etc. is demolished, and surplus concrete itself that occurs when the building, etc. is built, etc. It includes waste concrete (concrete waste) which is concrete, etc., expected to be disposed of in the future, and it is preferable to use these slag and waste concrete. Since the carbonate does not react with carbon dioxide in the air to further become a carbonate, it is excluded from compounds containing alkaline earth metals.\|[0028] The rock contains a compound containing an alkaline earth metal. That is, compounds such as Ca (calcium), Mg (magnesium), Be (beryllium), Sr (strontium), Ba (barium), and Ra (radium), which are alkaline earth metals, are cited, but it is preferable to use a compound of Ca (calcium) and Mg (magnesium), which is largely contained in natural rocks.\|[0029] The following is an example of a compound containing an alkaline earth metal. First, an oxide of a single alkaline earth metal is cited. For example, calcium oxide (CaO) which is an oxide of calcium, magnesium oxide (MgO) which is an oxide of magnesium, and the like can be used.\|[0030] Although barium oxide (BaO), which is an oxide of barium, strontium oxide (SrO), etc., which is an oxide of strontium, etc., it is preferable to use calcium oxide (CaO), magnesium oxide (MgO), which is an oxide of magnesium, etc.\|[0031] Other oxides include magnesium/iron oxides (MgFe2O4, etc.), calcium/iron oxides (Ca2Fe2O5, etc.), magnesium aluminate (magnesium alumina oxide) (MgAl2O4, etc.), calcium aluminate, and calcium oxide. An oxide such as calcium ferroaluminate can be used. For example, calcium aluminate such as Ca3Al2O6, Ca12Al14O33 or calcium iron aluminate such as Ca4Al2Fe2O10 can be used.\|[0032] As the compound, for example, calcium silicate can be used. For example, a calcium silicate such as Ca2SiO4, Ca3Si2O7, Ca3SiO5, CaSiO3 can be transferred.\|[0033] As the compound, for example, magnesium silicate or magnesium aluminosilicate can be used. For example, magnesium silicate such as MgSiO3 and Mg2SiO4 or magnesium aluminosilicate such as Mg3Al2Si3O12 can be used.\|[0034] As the compound, for example, calcium silicate magnesium can be used. For example, a calcium silicate magnesium such as CaMgSiO4, Ca3MgSi2O8, Ca7MgSi4O16, CaMgSi2O6, Ca2MgSi2O7, etc., can be used.\|[0035] As the compound, for example, calcium aluminosilicate can be used. For example, calcium aluminosilicate such as CaAl2Si2O8, Ca2Al2SiO7, Ca3Al2Si3 O12, etc., can be used.\|[0036] As the compound, for example, calcium silicate iron can be used. For example, CaFeSiO4, (Ca/Fe)SiO3, (Ca/Fe)2SiO4, Ca3Fe2Si3O12, CaFeSi2O6, Ca0.82Fe0.18SiO2, etc., Ca(Fe/Mg)Si2O6, Calcium iron silicate, calcium magnesium iron silicate, magnesium iron silicate, etc. can be used.\|[0037] For example, calcium silicate iron can be CaXFe2-XSiO4 (0<X<2). A compound obtained by substituting iron for the calcium silicate magnesium moiety or a compound obtained by substituting magnesium for the iron moiety of the calcium silicate iron may also be used.\|[0038] In the application of the present invention to a compound containing an alkaline earth metal, including the above-described compound, the reactivity of the original compound (i.e., difficulty in mineralizing carbon dioxide due to contact with carbon dioxide or difficulty in mineralizing carbon dioxide. This suggests that there is a difference in the reactivity when pulverized and atomized.\|[0039] Figures 1 and 2 show that the compounds listed in Figures 1 and 2 are selected from the above compounds, and pulverized so that their particle sizes are less than 3 μm. Assuming the temperature is 30°C and the relative humidity is 90%, the change in the mineralization effect (mineralization ratio (%)) of carbon dioxide (carbon dioxide concentration: 415ppm) in the atmosphere for the target compound is estimated to be 14 days old (the compound shown in Figure 1). The figure shows the results when the number of months elapsed is measured as December (one year) (the compound listed in Figure 2). Fig. 1 is referred to as "graph 1" and Fig. 2 is referred to as "graph 2".\|[0040] The mineralization ratio (%) is the actual mineralization amount of each compound relative to the CO2 (carbon dioxide) mineralization amount potential represented by formula (I) (see formula (II)). ).\|[0041] The CO2 mineralization potential indicates the amount of mineralization that is ideally achievable, and the mineralization rate (%), which is the ratio of the actual amount of mineralization to the potential, is an index indicating the degree of ease of mineralization (mineralization reaction).\|[0042] \|[0043] \|[0044] From Figures 1 and 2, the compounds listed in Figure 1 (CaO, MgO, Ca2SiO4, CaSiO3) have excellent reactivity and are shown to be highly reactive. (In Fig. 2, the lines of Mg2SiO4 and MgSiO3 results almost overlap. ). In addition to Figures 1 and 2, Table 1 shows that the CO2 mineralization potential (kg-CO2/kg) is determined by selecting the compounds listed in Table 1 from the above compounds. If the particle size of the crushed compound is 1 to 3 μm, the mineralization rate (%) after 1 year when it is 5 to 10 μm (Table 1 abbreviates "mineralization rate", but it is agreed with the mineralization rate (the same as the others). ) is shown.\|TABLE 1\|[0045] \|[0046] Although the above compound (mineral) is an example, it can be confirmed that the mineralization ratio of calcium oxide (CaO), magnesium oxide (MgO), calcium/iron oxide, calcium aluminate, and calcium silicate, which are oxides of alkaline earth metals, is high.\|[0047] From this result, it is preferable that the rocks used in the present invention contain these compounds, which are referred to as "Group 1" in Table 1 (corresponding to "Group 1" described below). ).\|[0048] 1, 2, and Table 1 indicate that these compounds have high mineralization rates (fast mineralization reaction) and, when contained in rocks, can form carbonates efficiently by contact with carbon dioxide in the air.\|[0049] According to the results of Table 1, etc., the compounds can be divided into the following groups 1 to 3. Each group is considered to have the following characteristics regarding mineralization.\|[0050] In addition, natural rocks, slag, waste concrete, etc., often contain compounds other than the above compounds, i.e., compounds not containing alkaline earth metals. For example, silicon oxide (SiO2), aluminum oxide (alumina) (Al2O3), aluminosilicate, iron oxide (FeO, Fe2O3, Fe3O4), and aluminum oxide are oxides. Compounds (minerals) such as manganese oxide (MnO), iron silicate (FeSiO3, Fe2SiO4), carbonate, and alkali minerals are enumerated. All of these are pulsate stones, which are essentially unnecessary compounds (ores).\|[0051] Compounds such as these compounds that do not contain alkaline earth metals, such as calcium and magnesium, do not form carbonates even when ground and brought into contact with carbon dioxide under prescribed conditions (Group 4). ). The group 4 also contains a compound which cannot form a carbonate under a predetermined condition.\|[0052] Based on the results of Table 1 and other data, Groups 1 through 4 are defined as follows by the degree of mineralization reaction.\|[0053] Group 1: Carbon dioxide mineralization is roughly completed (>95%) within 1 year if the particle size is crushed to 1 to 3 μm. When the particle size is crushed to 5 to 10 μm, it is 60% or more. Refers to compounds (minerals) that are considered possible (highly reactive compounds). For example, calcium oxide (CaO), Magnesium oxide (MgO), oxide of calcium/iron oxide (Ca2Fe2O5, etc.), Ca3Al2O6, Ca12. The composition contains at least one compound among calcium aluminate such as Al14O33 and calcium silicate such as Ca2SiO4, Ca3Si2O7, Ca3SiO5, and CaSiO3 The compounds, etc. listed in Group 1 in Table 1 are enumerated. Further, the compounds containing an alkaline earth metal, as described in the present invention, such as these compounds and the compounds of the second group, include compounds that are partially substituted with other elements and that are construed to belong to these compounds. Concretely, a compound such as calcium silicate, magnesium silicate or calcium magnesium silicate wherein a part of calcium ion or magnesium ion is replaced by iron ion may be used.\|[0054] Group 2: Compounds that, even when milled to 1 to 3 μm in particle size, are considered to have a carbon dioxide mineralization rate of 10 to 95% within 1 year (compounds with normal reactivity). For example, calcium ferrous aluminate such as Ca4Al2Fe2O10, magnesium silicate such as MgSiO3 and Mg2SiO4, calcium aluminosilicate such as CaMgSiO4, Ca3MgSi2O8, Ca2MgSi2O7, Ca7MgSi4O16, CaMgSi2O6, calcium silicate magnesium silicate such as Ca2Al2SiO7, CaAl2Si2O8, etc., and MgAl2O4. The term "A-" refers to amorphous (amorphous) compounds such as oxide (magnesium aluminate), magnesium/iron oxide such as MgFe2O4, A-CaMgSiO4, A-Ca2MgSi2O7, A-Ca3Si2O7, and A-CaSiO3. The same applies hereinafter. Table 1, Group 2 (2). Compounds listed in the table above are examples.\|[0055] Group 3: Refers to compounds (compounds with slightly lower reactivity) that are considered to have a carbon dioxide mineralization rate of less than 10% within 1 year, even if the particle size is crushed to 1 to 3 μm. For example, Group 3 (3 in Table 1 includes A-Ca3SiO5, A-CaAl2Si2O8, A-Ca2SiO4, A-MgSiO3, A-Ca2Al2SiO7, A-Ca3MgSi2O8, A-Ca7MgSi4O16, A-Ca2Fe2O5, A-CaMgSi2O6, etc. Compounds listed in the table above are examples.\|[0056] Group 4: Alkaline earth metals (calcium, magnesium, etc.) It is a compound that does not contain carbonic acid (including thrombophiles), or that is thought to be unable to form carbonic acid under ambient conditions. (Chemical compounds that cannot be expected to react). For example, silicon oxide (SiO2), aluminum oxide (alumina) (Al2O3), iron oxide (FeO, Fe3O4, Fe2O5, etc. Examples include manganese oxide (MnO), iron silicate (FeSiO3, Fe2SiO4), carbonate, and alkaline minerals.\|[0057] As the rocks to be applied to the method of the present invention, the ratio of the groups 1 to 4 is considered to be important. In the above group, the reactivity is highest when the group 1 is considered as a single compound and lowest when the group 4 is considered as a single compound (reactivity is Group 1>Group 2>Group 3>Group 4. ).\|[0058] It goes without saying that the composition of the rocks used is better if they have a high content of compounds belonging to the group with high reactivity. The range of the content of each group is shown below, but as described below, reactivity includes the presence of other components of the rock (natural rocks include the presence of pulsels, etc.). Therefore, the following range is only one criterion, because it depends on the particle size (particle size) obtained in the particle processing, the carbon dioxide concentration of the air in contact, etc.\|[0059] I would like to expect that the compounds belonging to Group 1 are present as much as possible in rocks compared with the compounds of other groups, but in the case of natural rocks, there are many cases where it is not known unless it is mined, so it cannot be determined uniformly.\|[0060] In consideration of such circumstances, the following compounds belong to Group 1: (i) Calcium oxide, Magnesium oxide, Calcium/Iron oxide, Calcium aluminate, Calcium silicate, etc. The rock preferably contains not less than 5% by mass relative to the whole rock, more preferably not less than 10% by mass, and particularly not less than 15% by mass. The more compounds in Group 1, such as all of the rocks (100% by mass) or more than 90% by mass of the whole rock, the better the mineralization performance of the rock. The content which can actually be expected is limited to about 25 mass%, and it is considered that 5 to 20 mass% should be contained. In addition, the compounds belonging to Group 1 are generally contained in an amount of 5 to 20 mass% relative to the total amount of the natural rocks when the compounds of Group 1 are present. In the case of slag, waste concrete, etc., the content is often 0 to 90 mass%.\|[0061] Compounds belonging to Group 2 (excluding those amorphized in Table 1) In the case of a rock containing a compound belonging to Group 1, it is preferable to contain as much of the remainder (generally 80-100 mass% of the remainder) excluding the compound belonging to Group 1 as possible, because the rock does not want to contain the compound belonging to Group 3 and Group 4 described below as much as possible.\|[0062] On the other hand, when not containing a compound belonging to Group 1, the compound belonging to Group 2 is preferably contained in an amount of 50 mass% or more, preferably in an amount of 70 mass% or more, and particularly preferably in an amount of 70-100 mass%, with respect to the whole rock. In the case of natural rocks, the amount of compounds belonging to Group 2 is approximately 70-100% by mass in total relative to the whole rock (in the case of no compounds belonging to Group 1, the amount of total compounds belonging to Group 1 is about 70-100% by mass in the case of natural rocks. When present, it is generally contained in an amount of 0 to 25 mass%. When used in slag, waste concrete, etc., it is often contained in an amount of 0 to 30 mass%.\|[0063] It is preferable that the compounds belonging to Group 3, Group 4 are not present as much as possible.\|[0064] When the rock is a natural rock, for example, magnesium oxide (MgO), calcium oxide (CaO), magnesium silicate, calcium silicate magnesium, and magnesium iron silicate can be mainly used in the present invention.\|[0065] Natural rocks, for example, igneous rocks, sedimentary rocks, metamorphic rocks, etc., are considered, but igneous rocks are preferably used. Although the igneous rock may be a deep rock, volcanic rock, etc., it is preferable to use the deep rock.\|[0066] From the content of SiO2, the rock is acidic (generally, the content of SiO2 exceeds 66 mass% of the whole). The SiO2 content is 52-66% by mass. Rock mass: 45-52% by mass (basic rock), 45-52% by mass (suprabasic rock), 45% by mass or less (basic rock). ) can be listed. In the present invention, it is preferable to use a suprabasic rock or a basic rock, and particularly preferable to use a suprabasic rock.\|[0067] Suprabasic rocks, also called suprapaceous rocks, are generally composed of ornithospherite, dang ornithospherite, serpentine, ornithospherite ornithospherite, monolithospherite ornithospherite, bibiornithospherite ornithospherite, komatiite, etc. Basic rocks are also called mafic rocks, and generally consist of mottled rocks, basaltic rocks, drylights, etc.\|[0068] The basic rock is composed mainly of magnesium silicate (magnesium silicate) and CaSi such as MgSiO3 (olivine) and Mg2SiO4 (olivine). Contains mgSi2O6 (pyroxite), and may also contain a silicated mineral such as CaAl2Si2O8. The magnesium silicate belongs to the group 2, and the mineralization reaction is not so fast.\|[0069] On the other hand, magnesium oxide (MgO) belonging to Group 1 and very fast mineralization reaction (generally considered to be about 0 to 10 mass% in general, but it is not limited to this range) is appropriate for the ultra-basic rock. It is considered that the total amount of the compounds in Group 1 is about 5 to 20 mass%. In addition, it is a natural rock suitable for mineralization because silica (SiO2) and alumina silicate are hardly contained in the suprabasic rock. In addition, ultrafine rocks are natural rocks that are widely available in large quantities.\|[0070] The basic rock is composed mainly of CaAl2Si2O8 and other suitable compounds. and CaMgSi2O6 (pyroxene). Magnesium silicate (magnesium silicate) such as MgSiO3 (talc), Mg2SiO4 (talc), etc. are also included.\|[0071] Rocks containing many amorphous (amorphous) compounds (rocks with a large amount of amorphous phase) have low reactivity and often interfere with mineralization. Since they envelop other crystals and are involved in the amorphous phase, they are connected to each other (it is important to advance the mineralization reaction). (This will prevent you from doing so.\|[0072] In the state of the rock before grinding, the amorphous portion of the rock (the rock having a large amount of an amorphous phase) containing a large amount of an amorphous compound is generally preferred to be 30 mass% or less. If the proportion of amorphous (amorphous) parts is 30 mass% or less, it is considered that completely enclosing the crystals is suppressed, even if the amorphous phase (amorphous part) may occupy the space between the crystalline minerals. The above range includes the presence of other components of the rock (natural rock includes the presence of pulsatile rocks, etc.). Therefore, the range of exposure depends on the particle size (particle size) and the carbon dioxide concentration of the air in contact with the particles.\|[0073] (A-2) Pulverization: In the case of natural rocks, the rock is mined and then pulverized to form fine particles. In the micronization process, the crystal state of each rock-forming compound is maintained (amorphous). (This is important.\|[0074] When the compound constituting the rock is pulverized into fine particles, the smaller the particle size, the larger the surface area of the fine particles and the larger the contact surface with air (carbon dioxide). However, if the particle size is too small, the rock becomes amorphous and the reactivity to mineralization decreases.\|[0075] Of the above compounds, the compounds listed in Table 2 are selected, and the approximate particle size (amorphous diameter) to be amorphous (amorphous diameter) when pulverized into fine particles is listed in Table 2. In addition, "grinding efficiency of each compound" and "effective rate of mineralization" are also listed in Table 2. In addition, the amorphization diameter shown in Table 2 is only a guide, and it does not reliably amorphize if it is below this diameter.\|TABLE 2\|[0076] \|[0077] The time t required for the reaction of the fine particles having a radius of R(m) to reach the depth δ is expressed in formula (III). The concentration of calcium (Ca) and magnesium (Mg) in a solid is ρ, the vapor phase concentration of CO2 is Cg, and the diffusion coefficient of ions through the product layer is D (m2/s).\|[0078] \|[0079] t: Time (sec) ρ: Sum of molar density of magnesium (Mg) and calcium (Ca) in rock (moles/m3-rock) R: Radius of fine particles (m) D: Concentration of CO in the compound Diffusion coefficient of CO2 (m2/s)Cg: CO2 molar concentration in gas phase (moles/m3-gas) δ: Reaction depth (m)\|[0080] On the other hand, if the radius (particle size) of the fine particles is too large, it takes a very long time for all of the fine particles to react, which is also undesirable. According to the unreacted nuclear model, the reaction rate is considered to be inversely proportional to the cube of the diameter of the particles. For example, if the crushing result is 6 μm as a result of assuming 3 μm, the reaction is considered to be 8 (23) times slower.\|[0081] The diffusion coefficient, D, represents the rate of CO2 diffusion through the product layer in the unreacted nuclear model (m2/s), and does not directly represent the mineralization rate of carbon dioxide because of other factors. Since diffusion through the product layer is a rate-limiting step of pneumonialization of CO2, a large diffusion coefficient D actually indicates a mineral that rapidly mineralizes carbon dioxide.\|[0082] The outer diameter (particle size) of the fine particles is determined by the mass of the compound belonging to the above group 1 relative to the total fine particles of the rock obtained. It is considered that the reaction proceeds without crushing the rock more finely than necessary, and that the generation of carbon dioxide by energy loss or crushing can be suppressed, and in addition, the amorphization of the rock (compound) can be suppressed.\|[0083] On the other hand, the reactivity of the whole rock is determined by the type of other components of the rock (natural rock includes the presence of pulsatile rocks, etc.). The composition of the rock may also be referred to as the "rock element", and the composition and composition of the crystalline layer and the amorphous phase, the relationship between the crystalline layer and the amorphous phase, and other factors such as the amount of carbon dioxide oxidation (hereinafter referred to as the "rock element") may also be used. The range of particle size of the crushed rock is also affected by these factors.\|[0084] In view of these facts, when microparticulating rocks, the particle size of the fine particles is generally preferably 100 μm or less (more preferably 50 μm or less, more preferably 25 μm or less, more preferably 10 μm or less. In consideration of the rock elements, appropriate selection may be made, for example, within the range of particle sizes of 1-25 μm, 1-20 μm, 1-10 μm, 1-5 μm, 1-3 μm, etc. For example, when a first group of highly reactive compounds is contained, the particle size may be 1-25 μm (preferably 1-10 μm).\|[0085] If the particle size is 1 to 3 μm, the surface area is large and good reactivity can be expected, but as shown in Table 2, if the particle size is made too small, amorphization may progress and the reactivity may actually become poor. Therefore, it is preferable to limit the particle size of 1 to 3 μm to about 1 to 10 μm or less with the target of 1 to 3 μm. Regarding the particle size of the fine particles, for example, the fine particles of the crushed rock can be spread so as not to overlap, the image acquired by the optical microscope or the like can be analyzed by a computer, and the particle diameter (particle diameter) and shape of the complete distribution of the fine particles can be determined (preferably, the maximum particle diameter is adopted. ). It is desirable that at least 5000 (or 10000) particles are analyzed for each sample of the compound.\|[0086] The rock crushing operation in the micronization can be performed by using a conventionally known crushing means, but, for example, it is preferable to perform the rock by using vertical roller mill, high pressure grinding rolls, etc. It should be noted that ball mills generally have low energy efficiency and tend to become amorphous.\|[0087] In the case of simply atomizing the rock, the rock may be put into a mortar and crushed by using a mortar and a scraper to obtain a desired particle size. In the crushing of rocks by mortar and mortar, for example, it is possible to achieve a very low degree of amorphization by separating very small fine particles that are expected to have been amorphized when they are produced and carrying out a minimum amount of crushing to achieve a desired particle size.\|[0088] Rock crushing prevents amorphization, reduces particle distribution (size distribution of fine particles) as much as possible, minimizes energy consumption (energy consumption generates carbon dioxide, and substantial carbon dioxide reduction is reduced. (3) should be taken into account. These are considered to be particles that have become too small (amorphous) while grinding, for example, using high-pressure grinding. Also, the load of the crusher can be reduced (energy efficiency can be increased) by separating. (This will be retained for the purpose of separation.) On the other hand, the low-pressure grinding (low-pressure grinding) is preferably ground by a vertical roller mill, which is considered to be an aspect of the high-pressure grinding means, because the supplied energy causes dislocation (amorphization) of the crystal structure and generation of heat and sound (energy loss).\|[0089] It is preferable to reduce (narrow) the particle distribution in rock crushing as much as possible. By narrowing the particle distribution, the air to be contacted to mineralize carbon dioxide diffuses into the particulate layer.\|[0090] Such diffusion is an important factor in CO2 mineralization, and it is considered inefficient that the wide particle distribution reduces the porosity between particles, and only the upper part of the ground layer comes into contact with CO2. Less diffusion means that the rock is spread into a thinner layer (the rock layer becomes thinner. It means that it is necessary. The thinning of the rock layer is undesirable because it reduces the amount of rock that can be processed per unit volume of the equipment and at the same time increases the number of sheets per unit rock, which increases the cost.\|[0091] A commercial air classifier or a sieve, etc., may be used for classification. A pulverizer having a classification function may also be used. The particle size distribution is performed by using a conventional technique (for example, measuring the classified fine particles by using an optical microscope equipped with a computer vision operated by commercial software). (You can use it to do this.\|[0092] For example, as also described in CaMgSiO4 in Table 1, there are cases where the compound that has become amorphous as a result of microparticle formation mineralizes CO2 more rapidly than a compound that is not amorphous (crystalline compound). In this case, since the structure of the amorphous compound changes depending on the ratio of the cation to the silica, certain compositions such as CaMgSiO4 favorably react with carbon dioxide even in the case of an amorphous structure and mineralization proceeds.\|[0093] On the other hand, such cases are an exception, and from the point of view of engineering, you will never find pure minerals, and there is always a certain degree of mixing and variation in composition. Therefore, the significant reduction in carbon dioxide mineralization associated with most amorphous compounds outweighs the small performance gains of some compounds. In other words, it is preferable to avoid amorphous compounds because the reaction rate with carbon dioxide and the rate of mineralization are likely to be very low.\|[0094] Further, it is preferable that the rock fine particles obtained by the micronization step are not present as much as possible in the rock fine particles, because the mineralization reaction cannot be expected for the group 4 (compound not expected to react) originally contained in the rock fine particles due to the amorphization of the rock or the amorphization of the rock fine particles together with the micronization. These are preferably about 80 mass% or less in total, and are particularly preferably 50 mass% or less.\|[0095] (B) Carbonate formation process: Fine particles of the rock obtained are brought into contact with air in a predetermined space, whereby carbonates are formed in the fine particles. In other words, carbon dioxide in the air reacts with the fine particles of the rock composed of the above composition, and carbonates (mainly carbonates such as calcium and magnesium) are formed on the surface of the fine particles or in the inside thereof. As a result, carbon dioxide in the air is removed.\|[0096] The space shall be in a state where air is constantly stable (such as stably supplying air containing carbon dioxide and maintaining the conditions described below for the period of implementation, etc.). However, such a stable state can be easily and reliably formed, and it is preferable to use the stone in the room. The space is preferably a closed space capable of supplying air at a certain frequency by ventilation or the like.\|[0097] The introduced air refers to air in general that contains carbon dioxide, for example, the atmosphere (carbon dioxide content is considered to be about 400 to 450 ppm. All gases that are considered to contain carbon dioxide (CO2), such as exhaust gas, can be used. There are also no restrictions on the CO2 concentration of the air in question.\|[0098] The space is conditioned to have a temperature of 15 to 50°C and a relative humidity of 50 to 100%. Both the temperature condition and the humidity condition are within the aforementioned ranges, so that carbon dioxide is mineralized efficiently. The temperature in the space is preferably 20-40°C, and is particularly preferably 30-35°C. The relative humidity is preferably 60-95%.\|[0099] The flow rate of air containing carbon dioxide in a space can be appropriately determined according to the concentration of carbon dioxide, the type and composition of rocks. For example, a natural suprabasic rock (ultrapascular stone) is used as a rock, and the air to be carbon dioxide removed is used as the atmosphere (the carbon dioxide content is at the same level as described above). In this case, it is preferable that the exposure rate be approximately 1 to 100mm/sec, and particularly preferably 1 to 10mm/sec. Since the fine particles of the rock have a small particle diameter and are pulverized, it is preferable to use the above level to prevent the scattering of the fine particles.\|[0100] In the space, the contact between the rock particles and the air is not particularly restricted, but for example, a tray or the like placed in the space may be placed in a container with a shallow bottom such as a tray having an arbitrary area, and spread in a laminar state over the entire bottom surface of the tray.\|[0101] When stratification of rock particles in this way, it is necessary to consider the diffusion of CO2 into the deepest part of the layer. When rocks are crushed to the micrometer level, the diffusion of carbon dioxide in the air spaces between the particles is considered to be due to molecular diffusion. Therefore, there is a concern that the accumulation of fine rock particles in a thick layer decreases the concentration of carbon dioxide at the lower part (deep part) of the fine rock particles and slows the mineralization reaction. On the other hand, the degree of this deep region depends on the type of rock (compound), the size of the space, the particle size of the fine particles, the flow velocity of the air, etc.\|[0102] Based on the above, the thickness of the rock fine particles (fine particle layer) when spread in a layered state is, for example, preferably 5 cm (50 mm) or less, preferably 1-50 mm, more preferably 1-20 mm, more preferably 1-10 mm, and more preferably 1-5 mm.\|[0103] When the fine particles are put in the tray or the like and brought into contact with the air in the state of spreading the tray or the like in a layered state, the tray or the like may be mounted in a multistage in the height direction in the space.\|[0104] The contact time (reaction time) of air and rock particles. However, as a guide, it can be arbitrarily selected as 7 days to 1 year, for example, between 7 days and 2 months. Depending on the amount and type of rocks, the mineralization reaction is considered to have been completed approximately one year after the contact (mineralization reaction) began.\|[0105] When carbonates are formed in the fine particles of rock and carbon dioxide is mineralized, carbonates are accumulated on the surface of the rock, and the mass of fine particles of rock in which a large number of fine particles are assembled is first heated at less than 100°C to remove the adsorbed water. This procedure and the analytical procedures described below are not necessary if the generated carbonate, etc. are not analyzed.\|[0106] After the water is removed, the amount of mineralized carbon dioxide can be confirmed by comparing the mass change with the mass of the fine particles of the rock before the carbonate formation process as an analytical operation. In addition, carbon dioxide mineralized by thermogravimetric differential thermal analysis (TG-DTA) and X-ray fluorescence analysis (XRF) can be analyzed in detail such as the amount of carbon dioxide (carbonate).\|[0107] In addition, environmentally-harmless carbonates (mainly calcium and magnesium carbonate such as calcium carbonate (CaCO3 and MgCO3). The mineralized rocks can be used, for example, as subbase materials or construction materials for landfill. Thus, the mineralized rocks are environmentally friendly.\|[0108] (C) Effect of the present invention: The present invention is such that carbon dioxide in the air is mineralized as a carbonate by micronizing rocks containing alkaline earth metals and bringing the obtained microparticles into contact with air in a space having a predetermined environment, thereby fixing carbon dioxide to the rocks and removing carbon dioxide in the air.\|[0109] Consequently, the present invention can easily remove carbon dioxide from the air at low cost without using a chemical or using a large-scale facility, etc., and can substantially reduce carbon dioxide because the amount of carbon dioxide generated is small. In addition, there is no need of storing carbon dioxide, and there is no risk in such storage, and the immobilized carbon dioxide becomes a carbonate harmless to the environment, and can be reused together with rocks, so that it is also environmentally friendly.\|[0110] According to the present invention, CDR. can be performed without relying on other technologies and infrastructure. Conventional technologies require a large amount of energy to remove carbon dioxide from the air, and considering the carbon dioxide generated by such energy, many of the technologies have not reduced carbon dioxide substantially. On the other hand, the present invention removes carbon dioxide from the air by a simple method, i.e., a step for atomizing rocks and a step for forming a carbonate by reacting the obtained rock particulates with carbon dioxide in the air. Therefore, the present invention is considered to be a technology that requires less energy and leads to a substantial reduction in carbon dioxide.\|[0111] There are currently two main types of CDRs. These are Bioenergy with Carbon Capture and Storage (BECCS) with carbon dioxide (CO2) recovery and storage, and direct air recovery with carbon dioxide storage (DIRECT Air CO2 Capture with Storage:DACCS).\|[0112] Of these, BECCS relies on biomass combustion, carbon dioxide capture, transport to storage sites, and underground storage. The DACCS also uses machinery to filter carbon dioxide from the air before transport and underground storage. The main points to compare are energy requirements (GJ/t-CO2), land requirements (km2/Mt-CO2), water requirements (m3/t-CO2), the time required for CO2 recovery, biological restrictions (Gt-CO2/year), and cost. In all of these cases, t-CO2 means net carbon dioxide (CO2) removed from the environment (accounting for carbon dioxide emissions from processes and supply chains). ). Table 3 shows the comparison of the present invention and these two technologies. Table 3 confirms that the present invention works more advantageously than other technologies.\|TABLE 3\|[0113] \|[0114] In addition, there are scale-up and scale-out ratio issues. BECCS and DACCS usually limit their use to very large (>1Mt-CO2/year) reservoirs because they require reservoirs and transport infrastructure, and development of reservoirs is costly. On the other hand, the present invention can be applied at any scale, whether in the kg scale or in the Mt scale. Therefore, it is considered that small, medium and large-scale systems can be developed without worrying about transportation, storage, etc.\|[0115] In addition, it is not possible to accurately quantify the amount of CO2 removed by other methods using soil and oceans, and there is also the problem that such other methods may lose future CO2 expected due to the impact of climate change. Since carbon dioxide is immobilized as a carbonate by the above simple means and removed from the air, these problems can also be solved.\|[0116] (D) Variations of embodiments: The embodiments described above represent one aspect of the present invention, and the present invention is not limited to the aforementioned embodiments. Needless to say, the content of the present invention includes variations and improvements provided in the configuration of the present invention and to the extent that the purpose and effects can be achieved. The specific structure, shape, etc. in implementing the present invention are acceptable as other structures, shapes, etc., to the extent that the purpose and effect of the present invention can be achieved. The present invention is not limited to each of the embodiments described above, and any deformation or improvement within the scope of achieving the purpose of the present invention is included in the present invention.\|[0117] For example, although necessary operations for (A) the micronization step and (B) the carbonate formation step are partially illustrated, there is no problem with using other procedures not illustrated, to the extent that they do not interfere with the purpose and effect of the present invention. Similarly, a compound capable of constituting a rock is listed as an example, but since it is only an example, there is no problem in including other compounds in the rock used in the present invention, such as a compound containing an alkaline earth metal. Other specific structures, shapes, etc., in the implementation of the present invention may be other structures, etc., to the extent that the purpose of the present invention can be achieved.\|EMBODIMENTS EXAMPLE\|[0118] The present invention is described in more detail below based on examples, etc., but the present invention is not limited to these.\|[0119] (Reference Example 1, Examples 2 to 6, Reference Example 7, Example 8) The composition shown in Table 4 below (Analytical Means of Compound Composition, etc. are described below as equivalent to rock. 8 types of slag (Example 1 to Example 8 (Example 1, Example 2 to Example 6, Example 7, and Example 8) (Prepared). In addition, "%" indicates the content (mass%) to the whole.\|[0120] (Composition of Slag)\|TABLE 4\|[0121] Slag 1 to slag 8 were ground using a mortar and a scraper, and the ground slag was classified using a sieve. The particle size distribution of the slag particles after classification was measured using an optical microscope equipped with a computer vision operated by "ImageJ" software, which is one of the image processing techniques, and a particle sample with a particle size of 25-90 μm and a particle sample with a particle size of less than 25 μm were obtained respectively. In addition, the elemental compositions of slag (1-8) and the compound compositions of slag (1-8) were analyzed by XRF and Q-XRD, respectively (the compound compositions, etc. are shown in Table 4. ).\|[0122] The obtained fine particle samples were placed in a circular tray of 10cm diameter x 1 cm height respectively, and spread so that the thickness becomes 3 mm.\|[0123] The indoor space of a 22L-volume incubator (3-6815-01 CO2 incubator: made by Azwan Co., Ltd.) was set to have a relative humidity of 90% and a temperature of 30°C. Under such a humidity and temperature, a tray containing a particulate sample is placed in the indoor space of the incubator, the door is closed and sealed, and then air having a carbon dioxide concentration of 5% (slag 1-slag 5) and air having a carbon dioxide concentration of 20% (slag 5-slag 8) are introduced. Air was brought into contact with the particulate samples to mineralize carbon dioxide (form carbonate) so as to maintain this state. The test was performed on 1, 3, 7, 14, 21, and 28 days after the start of study treatment. ). Each sample was tested 3 times (n = 3) (Table 5 shows the mean values. ).\|[0124] After the number of days had elapsed, the particulate samples were measured in mass and carbon dioxide (carbonate) mineralized by thermogravimetric differential thermal analysis (TG-DTA) and X-ray fluorescence analysis (XRF) were analyzed. Table 5 and Table 6 show the mineralization ratio (%) of carbon dioxide corresponding to the number of days elapsed (the experimental value is Table 5, but the predicted value is listed in Table 6 as a reference. ). Two carbon dioxide concentrations were evaluated to confirm the unreacted nuclear model.\|TABLE 5\|[0125] \|TABLE 6\|[0126] \|[0127] From the results of Table 5, firstly, the mineralization ratio of slag 1 and slag 7 is very low (for example, 1% or less under the conducted carbon dioxide concentration conditions (slag 1 is 28 days old, slag 7 is 7 days old). ) can be confirmed. The reason for this is that both slag 1 and slag 7 are originally amorphous phases (amorphous parts). The same applies hereinafter. It is considered that the slag 1 and the slag 7 contain 34.1% and 100%, respectively. Since all (100%) of the slag 7 is an amorphous phase, the mineralization ratio is considered to be low.\|[0128] In the case of the slag (1), on the other hand, the amorphous phase accounts for 34.1% of the total amount, but the amorphous phase still accounts for a high percentage of the total amount. Therefore, crystals are trapped in the amorphous phase, and the crystals are not connected to each other, and only the crystals on the surface react, and therefore the mineralization ratio is considered to be low.\|[0129] Generally, when molten rock (natural rock or slag) is cooled, crystalline or amorphous compounds are formed, but rapid cooling tends to produce amorphous compounds, and slow cooling tends to produce crystals. The distribution of nucleation crystals in molten rock is random, and these crystals grow until they come into contact with other crystals. On the other hand, in the liquid phase between the crystals, if the crystals have solidified as an amorphous phase before growing together, the crystals are separated from each other and cannot be connected. Such an arrangement would hinder the progress of the mineralization of carbon dioxide.\|[0130] In addition, slag 1 and slags other than slag 7 (slags 2 to 6, slags 8) also contained an appropriate amount of amorphous phase. The above behavior was not observed, and the results in Table 5 confirmed that mineralization also progressed well (for example, mineralization rate is 5% or more when the number of days elapsed is 7 under the conducted carbon dioxide concentration conditions. ). This is probably because the amorphous phase occupied the space between the crystalline minerals but did not completely envelop the crystals.\|[0131] The slag (slag 2, slag 4, slag 6, and slag 8) containing a compound such as calcium oxide (oxide) belonging to the group 1 shows mineralization of carbon dioxide at an initial stage. In particular, the rapid mineralization of slag 2 and slag 4 is characterized by the calcium content mainly in oxide form (CaO and Ca2Fe2O5) and calcium silicate (both belong to Group 1). It is considered to be caused by the above.\|[0132] On the other hand, the mineralization ratio of the slag 3 and the slag 5 is relatively lower than that of the slag 3 and the slag 5, because the mixed cation silicate belonging to the group 2 is substituted with Mg or Fe to some extent. It is also considered that there are compounds belonging to Group 4.\|INDUSTRIAL APPLICABILITY\|[0133] The present invention can be advantageously used as a means for providing a technique that enables carbon dioxide in the air to be immobilized as a carbonate on a rock to reduce carbon dioxide in the air, and has high industrial applicability.	(JP7699796)\|TECHNICAL FIELD\|[0001] The present invention relates to a method for removing carbon dioxide from air. More specifically disclosed is a method for removing carbon dioxide from the air, which enables the conversion of carbon dioxide from the air into a useful and harmless state by mineralizing carbon dioxide as a carbonate.\|BACKGROUND ART\|[0002] It is obvious that carbon dioxide emitted into the atmosphere is the cause of global warming, which has been a problem in recent years. Reducing such carbon dioxide emissions is a major challenge in protecting the global environment.\|[0003] Carbon dioxide is naturally captured from the atmosphere through biological processes such as photosynthesis by plant life on land and in the ocean, but the concentration of carbon dioxide in the atmosphere continues to rise. Carbon dioxide is also said to be a factor in the acidification of the world's oceans, which poses a threat to marine ecosystems. On the other hand, systems for fixing and removing exhaust fumes from factories and carbon dioxide (CO2) gas in the atmosphere have been proposed in various ways (for example, see Patent Document 1, etc.). ).\|[0004] Net reduction of global carbon dioxide (CO2) concentrations to eliminate or reduce atmospheric CO2 is It is referred to as NET (Negative Emission Technology) or Carbon Dioxide Removal (CDR.) and various technologies are available (see, for example, Non-Patent Document 1 or Non-Patent Document 3). ).\|[0005] The carbon dioxide emitted must be removed from the atmosphere to stabilize the Earth's climate within a range compatible with modern civilization. Also, in general, the techniques described in the literature described above should be applied to biological systems (e.g., retention of carbon dioxide in soil, plants, or the ocean). ) or highly industrialized machinery that filters carbon dioxide from the air, liquefies it, and stores it underground. And, there was a tendency that chemicals, high temperature and special reactor were required for industrial process which depended on such machinery.\|CITATION LIST\|PATENT LITERATURE\|[0006] Special Report No. 2013-504424\|NON PATENT LITERATURE\|[0007] Nduagu, E., Bergerson, J. and Zevenhoven, R., 2012. Life cycle assessment of CO2 sequestration in magnesium silicate rock A comparative study. Energy Conversion and Management, 55, pp.116-126.\|Ncongwane, M.s., Broadhurst, J.L. and Petersen, J., 2018. Assessment of the potential carbon footprint of engineered processes fwor the mineral carbonation of PGM tailings. International Journal of Greenhouse Gas Control, 77, pp.70-81.\|Keller, d.P., Lenton, A., Littleton, E.w., Oschlies, A., Scott, v. and Vaughan, N.E., 2018. The effects of carbon dioxide removal on the carbon cycle. Current climate change reports, 4(3), pp.250-265.\|DISCLOSURE\|TECHNICAL PROBLEM\|[0008] Carbon dioxide mineralization in rocks occurs naturally over hundreds of thousands of years. However, conventional methods to promote the reaction are high temperature and high pressure, or by adding chemicals. On the other hand, such a method does not reduce greenhouse gases because it has a large energy load and a large amount of carbon dioxide emissions.\|[0009] Concretely, the technology disclosed in the non-patent document 1 has a problem that the substantial reduction in carbon dioxide amount is reduced because carbon dioxide is reacted with carbon dioxide under high temperature and high pressure conditions. In addition, the technology disclosed in Non-Patent Document 2 requires the addition of chemicals and background emissions during its production (e.g., carbon dioxide emissions related to the creation, transportation, termination and disposal of chemicals and additives). As with the technology disclosed in Non-Patent Document 1, substantial CO2 reductions were reduced by the use of CO2-P-P (Carbon Dioxide Reduction Method).\|[0010] Furthermore, the method disclosed in the non-patent document 3 is a method for simply dispersing crushed rocks on the soil surface, which is undesirable because it is difficult to estimate the amount of carbon dioxide mineralization and may adversely affect the environment.\|[0011] The direct removal of carbon dioxide from the atmosphere is only a part of the total amount of carbon dioxide removal (CDR.) that has already been released, which is in line with the climate change reduction target. The removed carbon dioxide must be transported to the appropriate location for disposal and stored deep underground in certain geological structures. These transport and storage systems are too large and costly for individual companies to manufacture and operate, and there are various political, economic, and social risks associated with achieving CDR. dependent on systems that store carbon dioxide underground.\|[0012] The present invention provides an environmentally friendly method for removing carbon dioxide from the air, the method being implemented at a low cost, being capable of substantially reducing carbon dioxide, and being free from the risk of carbon dioxide retention.\|TECHNICAL SOLUTION\|[0013] The method for removing carbon dioxide from the air according to the present invention is a method for removing carbon dioxide from the air, wherein a compound (excluding a carbonate) contains at least one of Ca (calcium) and Mg (magnesium). of rock to obtain fine particles of the rock; and The method includes a carbonate formation step in which the fine particles of the rock thus obtained are brought into contact with air in a space having a temperature of 15-50°C and a relative humidity of 50-100%, and carbonates are formed in the fine particles of the rock The amorphous portion of the rock is 30 mass% or less of the whole, and the fine particles of the rock have a particle diameter of 1-100 μm The fine particles of the rock are put in the tray in a state of spreading in a laminar state over the entire bottom surface of the tray. The rock is characterized in that the rock particles which are brought into contact with the air by placing the tray in the space and spread in the layer form have a thickness of 1 to 50 mm.\|[0014] The method for removing carbon dioxide from the air is characterized in that the rock contains at least one compound from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|[0015] The method for removing carbon dioxide from the air is characterized in that the rock contains, in a total amount, 5 mass% or more of at least one compound from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|[0017] The method for removing carbon dioxide from the air is characterized in that the rock contains at least one member selected from among ultra-basic rock, basic rock, slag and waste concrete.\|ADVANTAGEOUS EFFECTS\|[0020] The present invention secures carbon dioxide to a rock and removes carbon dioxide from the air by atomizing the rock containing an alkaline earth metal, bringing the obtained particulates into contact with air in a space having a predetermined environment, and mineralizing carbon dioxide in the air as a carbonate.\|[0021] Consequently, the present invention can easily remove carbon dioxide from the air at low cost without using a chemical or using a large-scale facility, etc., and can substantially reduce carbon dioxide because the amount of carbon dioxide generated is small. In addition, there is no need of storing carbon dioxide, and there is no risk in such storage, and the immobilized carbon dioxide becomes a carbonate harmless to the environment, and can be reused together with rocks, so that it is also environmentally friendly.\|DESCRIPTION OF DRAWINGS\|[0022] This chart (Graph 1) shows the change in the mineralization effect (mineralization rate (%)) of carbon dioxide in the atmosphere as a result of measuring the number of elapsed days as 14 days.\| This chart (Graph 2) shows the change in the mineralization effect (mineralization rate (%)) of carbon dioxide in the atmosphere as the number of months in December (one year).\|DESCRIPTION OF EMBODIMENTS\|[0023] An aspect of the present invention is explained below. The method for removing carbon dioxide from the air according to the present invention comprises atomizing a rock containing an alkaline earth metal ((I) atomization step) and bringing the atomized rock into contact with the air in a space having a specific environment Carbon dioxide in the air is mineralized and fixed by using carbon dioxide in the air as a carbonate ((II) carbonate formation process) to remove the carbon dioxide from the air.\|[0024] Step (A): In the step of atomizing, the rock is pulverized to obtain fine particles.\|[0025] (A-1) About rocks: First, I will explain available rocks. Any of natural and man-made rocks can be used as rocks if they are formed from the compounds, etc. shown below. In the present invention, the term "compound" also includes "mineral".\|[0026] Usable rocks are, for example, 0-100°C temperature, suitable moisture (for example, relative humidity of reaction environment is 50-100%, etc.). It is required that the formation of carbonate by reaction with gas phase carbon dioxide under atmospheric pressure is thermodynamically possible. The term "thermodynamically" is taken to mean that 0-dimensional calculation conditions are considered and meso-scale structures are not considered.\|[0027] The rocks usable in the present invention are so-called slags (steel slags, iron slag, etc.), which are composed of a substance containing a mineral component of an ore matrix, etc., which has been separated by melting from a metal to be metallurgically measured, when smelting the metal from the ore, etc., as rocks containing a compound containing an alkaline earth metal. In addition, concrete that was originally used for buildings, etc., such as demolished concrete that is created when the building itself is no longer necessary or when the building, etc. that used the building, etc. is demolished, and surplus concrete itself that occurs when the building, etc. is built, etc. It includes waste concrete (concrete waste) which is concrete, etc., expected to be disposed of in the future, and it is preferable to use these slag and waste concrete. Since the carbonate does not react with carbon dioxide in the air to further become a carbonate, it is excluded from compounds containing alkaline earth metals.\|[0028] The rock contains a compound containing an alkaline earth metal. That is, compounds such as Ca (calcium), Mg (magnesium), Be (beryllium), Sr (strontium), Ba (barium), and Ra (radium), which are alkaline earth metals, are cited, but it is preferable to use a compound of Ca (calcium) and Mg (magnesium), which is largely contained in natural rocks.\|[0029] The following is an example of a compound containing an alkaline earth metal. First, an oxide of a single alkaline earth metal is cited. For example, calcium oxide (CaO) which is an oxide of calcium, magnesium oxide (MgO) which is an oxide of magnesium, and the like can be used.\|[0030] Although barium oxide (BaO), which is an oxide of barium, strontium oxide (SrO), etc., which is an oxide of strontium, etc., it is preferable to use calcium oxide (CaO), magnesium oxide (MgO), which is an oxide of magnesium, etc.\|[0031] Other oxides include magnesium/iron oxides (MgFe2O4, etc.), calcium/iron oxides (Ca2Fe2O5, etc.), magnesium aluminate (magnesium alumina oxide) (MgAl2O4, etc.), calcium aluminate, and calcium oxide. An oxide such as calcium ferroaluminate can be used. For example, calcium aluminate such as Ca3Al2O6, Ca12Al14O33 or calcium iron aluminate such as Ca4Al2Fe2O10 can be used.\|[0032] As the compound, for example, calcium silicate can be used. For example, a calcium silicate such as Ca2SiO4, Ca3Si2O7, Ca3SiO5, CaSiO3 can be transferred.\|[0033] As the compound, for example, magnesium silicate or magnesium aluminosilicate can be used. For example, magnesium silicate such as MgSiO3 and Mg2SiO4 or magnesium aluminosilicate such as Mg3Al2Si3O12 can be used.\|[0034] As the compound, for example, calcium silicate magnesium can be used. For example, a calcium silicate magnesium such as CaMgSiO4, Ca3MgSi2O8, Ca7MgSi4O16, CaMgSi2O6, Ca2MgSi2O7, etc., can be used.\|[0035] As the compound, for example, calcium aluminosilicate can be used. For example, calcium aluminosilicate such as CaAl2Si2O8, Ca2Al2SiO7, Ca3Al2Si3 O12, etc., can be used.\|[0036] As the compound, for example, calcium silicate iron can be used. For example, CaFeSiO4, (Ca/Fe)SiO3, (Ca/Fe)2SiO4, Ca3Fe2Si3O12, CaFeSi2O6, Ca0.82Fe0.18SiO2, etc., Ca(Fe/Mg)Si2O6, Calcium iron silicate, calcium magnesium iron silicate, magnesium iron silicate, etc. can be used.\|[0037] For example, calcium silicate iron can be CaXFe2-XSiO4 (0<X<2). A compound obtained by substituting iron for the calcium silicate magnesium moiety or a compound obtained by substituting magnesium for the iron moiety of the calcium silicate iron may also be used.\|[0038] In the application of the present invention to a compound containing an alkaline earth metal, including the above-described compound, the reactivity of the original compound (i.e., difficulty in mineralizing carbon dioxide due to contact with carbon dioxide or difficulty in mineralizing carbon dioxide. This suggests that there is a difference in the reactivity when pulverized and atomized.\|[0039] Figures 1 and 2 show that the compounds listed in Figures 1 and 2 are selected from the above compounds, and pulverized so that their particle sizes are less than 3 μm. Assuming the temperature is 30°C and the relative humidity is 90%, the change in the mineralization effect (mineralization ratio (%)) of carbon dioxide (carbon dioxide concentration: 415ppm) in the atmosphere for the target compound is estimated to be 14 days old (the compound shown in Figure 1). The figure shows the results when the number of months elapsed is measured as December (one year) (the compound listed in Figure 2). Fig. 1 is referred to as "graph 1" and Fig. 2 is referred to as "graph 2".\|[0040] The mineralization ratio (%) is the actual mineralization amount of each compound relative to the CO2 (carbon dioxide) mineralization amount potential represented by formula (I) (see formula (II)). ).\|[0041] The CO2 mineralization potential indicates the amount of mineralization that is ideally achievable, and the mineralization rate (%), which is the ratio of the actual amount of mineralization to the potential, is an index indicating the degree of ease of mineralization (mineralization reaction).\|[0042] \|[0043] \|[0044] From Figures 1 and 2, the compounds listed in Figure 1 (CaO, MgO, Ca2SiO4, CaSiO3) have excellent reactivity and are shown to be highly reactive. (In Fig. 2, the lines of Mg2SiO4 and MgSiO3 results almost overlap. ). In addition to Figures 1 and 2, Table 1 shows that the CO2 mineralization potential (kg-CO2/kg) is determined by selecting the compounds listed in Table 1 from the above compounds. If the particle size of the crushed compound is 1 to 3 μm, the mineralization rate (%) after 1 year when it is 5 to 10 μm (Table 1 abbreviates "mineralization rate", but it is agreed with the mineralization rate (the same as the others). ) is shown.\|TABLE 1\|[0045] \|[0046] Although the above compound (mineral) is an example, it can be confirmed that the mineralization ratio of calcium oxide (CaO), magnesium oxide (MgO), calcium/iron oxide, calcium aluminate, and calcium silicate, which are oxides of alkaline earth metals, is high.\|[0047] From this result, it is preferable that the rocks used in the present invention contain these compounds, which are referred to as "Group 1" in Table 1 (corresponding to "Group 1" described below). ).\|[0048] 1, 2, and Table 1 indicate that these compounds have high mineralization rates (fast mineralization reaction) and, when contained in rocks, can form carbonates efficiently by contact with carbon dioxide in the air.\|[0049] According to the results of Table 1, etc., the compounds can be divided into the following groups 1 to 3. Each group is considered to have the following characteristics regarding mineralization.\|[0050] In addition, natural rocks, slag, waste concrete, etc., often contain compounds other than the above compounds, i.e., compounds not containing alkaline earth metals. For example, silicon oxide (SiO2), aluminum oxide (alumina) (Al2O3), aluminosilicate, iron oxide (FeO, Fe2O3, Fe3O4), and aluminum oxide are oxides. Compounds (minerals) such as manganese oxide (MnO), iron silicate (FeSiO3, Fe2SiO4), carbonate, and alkali minerals are enumerated. All of these are pulsate stones, which are essentially unnecessary compounds (ores).\|[0051] Compounds such as these compounds that do not contain alkaline earth metals, such as calcium and magnesium, do not form carbonates even when ground and brought into contact with carbon dioxide under prescribed conditions (Group 4). ). The group 4 also contains a compound which cannot form a carbonate under a predetermined condition.\|[0052] Based on the results of Table 1 and other data, Groups 1 through 4 are defined as follows by the degree of mineralization reaction.\|[0053] Group 1: Carbon dioxide mineralization is roughly completed (>95%) within 1 year if the particle size is crushed to 1 to 3 μm. When the particle size is crushed to 5 to 10 μm, it is 60% or more. Refers to compounds (minerals) that are considered possible (highly reactive compounds). For example, calcium oxide (CaO), Magnesium oxide (MgO), oxide of calcium/iron oxide (Ca2Fe2O5, etc.), Ca3Al2O6, Ca12. The composition contains at least one compound among calcium aluminate such as Al14O33 and calcium silicate such as Ca2SiO4, Ca3Si2O7, Ca3SiO5, and CaSiO3 The compounds, etc. listed in Group 1 in Table 1 are enumerated. Further, the compounds containing an alkaline earth metal, as described in the present invention, such as these compounds and the compounds of the second group, include compounds that are partially substituted with other elements and that are construed to belong to these compounds. Concretely, a compound such as calcium silicate, magnesium silicate or calcium magnesium silicate wherein a part of calcium ion or magnesium ion is replaced by iron ion may be used.\|[0054] Group 2: Compounds that, even when milled to 1 to 3 μm in particle size, are considered to have a carbon dioxide mineralization rate of 10 to 95% within 1 year (compounds with normal reactivity). For example, calcium ferrous aluminate such as Ca4Al2Fe2O10, magnesium silicate such as MgSiO3 and Mg2SiO4, calcium aluminosilicate such as CaMgSiO4, Ca3MgSi2O8, Ca2MgSi2O7, Ca7MgSi4O16, CaMgSi2O6, calcium silicate magnesium silicate such as Ca2Al2SiO7, CaAl2Si2O8, etc., and MgAl2O4. The term "A-" refers to amorphous (amorphous) compounds such as oxide (magnesium aluminate), magnesium/iron oxide such as MgFe2O4, A-CaMgSiO4, A-Ca2MgSi2O7, A-Ca3Si2O7, and A-CaSiO3. The same applies hereinafter. Table 1, Group 2 (2). Compounds listed in the table above are examples.\|[0055] Group 3: Refers to compounds (compounds with slightly lower reactivity) that are considered to have a carbon dioxide mineralization rate of less than 10% within 1 year, even if the particle size is crushed to 1 to 3 μm. For example, Group 3 (3 in Table 1 includes A-Ca3SiO5, A-CaAl2Si2O8, A-Ca2SiO4, A-MgSiO3, A-Ca2Al2SiO7, A-Ca3MgSi2O8, A-Ca7MgSi4O16, A-Ca2Fe2O5, A-CaMgSi2O6, etc. Compounds listed in the table above are examples.\|[0056] Group 4: Alkaline earth metals (calcium, magnesium, etc.) It is a compound that does not contain carbonic acid (including thrombophiles), or that is thought to be unable to form carbonic acid under ambient conditions. (Chemical compounds that cannot be expected to react). For example, silicon oxide (SiO2), aluminum oxide (alumina) (Al2O3), iron oxide (FeO, Fe3O4, Fe2O5, etc. Examples include manganese oxide (MnO), iron silicate (FeSiO3, Fe2SiO4), carbonate, and alkaline minerals.\|[0057] As the rocks to be applied to the method of the present invention, the ratio of the groups 1 to 4 is considered to be important. In the above group, the reactivity is highest when the group 1 is considered as a single compound and lowest when the group 4 is considered as a single compound (reactivity is Group 1>Group 2>Group 3>Group 4. ).\|[0058] It goes without saying that the composition of the rocks used is better if they have a high content of compounds belonging to the group with high reactivity. The range of the content of each group is shown below, but as described below, reactivity includes the presence of other components of the rock (natural rocks include the presence of pulsels, etc.). Therefore, the following range is only one criterion, because it depends on the particle size (particle size) obtained in the particle processing, the carbon dioxide concentration of the air in contact, etc.\|[0059] I would like to expect that the compounds belonging to Group 1 are present as much as possible in rocks compared with the compounds of other groups, but in the case of natural rocks, there are many cases where it is not known unless it is mined, so it cannot be determined uniformly.\|[0060] In consideration of such circumstances, the following compounds belong to Group 1: (i) Calcium oxide, Magnesium oxide, Calcium/Iron oxide, Calcium aluminate, Calcium silicate, etc. The rock preferably contains not less than 5% by mass relative to the whole rock, more preferably not less than 10% by mass, and particularly not less than 15% by mass. The more compounds in Group 1, such as all of the rocks (100% by mass) or more than 90% by mass of the whole rock, the better the mineralization performance of the rock. The content which can actually be expected is limited to about 25 mass%, and it is considered that 5 to 20 mass% should be contained. In addition, the compounds belonging to Group 1 are generally contained in an amount of 5 to 20 mass% relative to the total amount of the natural rocks when the compounds of Group 1 are present. In the case of slag, waste concrete, etc., the content is often 0 to 90 mass%.\|[0061] Compounds belonging to Group 2 (excluding those amorphized in Table 1) In the case of a rock containing a compound belonging to Group 1, it is preferable to contain as much of the remainder (generally 80-100 mass% of the remainder) excluding the compound belonging to Group 1 as possible, because the rock does not want to contain the compound belonging to Group 3 and Group 4 described below as much as possible.\|[0062] On the other hand, when not containing a compound belonging to Group 1, the compound belonging to Group 2 is preferably contained in an amount of 50 mass% or more, preferably in an amount of 70 mass% or more, and particularly preferably in an amount of 70-100 mass%, with respect to the whole rock. In the case of natural rocks, the amount of compounds belonging to Group 2 is approximately 70-100% by mass in total relative to the whole rock (in the case of no compounds belonging to Group 1, the amount of total compounds belonging to Group 1 is about 70-100% by mass in the case of natural rocks. When present, it is generally contained in an amount of 0 to 25 mass%. When used in slag, waste concrete, etc., it is often contained in an amount of 0 to 30 mass%.\|[0063] It is preferable that the compounds belonging to Group 3, Group 4 are not present as much as possible.\|[0064] When the rock is a natural rock, for example, magnesium oxide (MgO), calcium oxide (CaO), magnesium silicate, calcium silicate magnesium, and magnesium iron silicate can be mainly used in the present invention.\|[0065] Natural rocks, for example, igneous rocks, sedimentary rocks, metamorphic rocks, etc., are considered, but igneous rocks are preferably used. Although the igneous rock may be a deep rock, volcanic rock, etc., it is preferable to use the deep rock.\|[0066] From the content of SiO2, the rock is acidic (generally, the content of SiO2 exceeds 66 mass% of the whole). The SiO2 content is 52-66% by mass. Rock mass: 45-52% by mass (basic rock), 45-52% by mass (suprabasic rock), 45% by mass or less (basic rock). ) can be listed. In the present invention, it is preferable to use a suprabasic rock or a basic rock, and particularly preferable to use a suprabasic rock.\|[0067] Suprabasic rocks, also called suprapaceous rocks, are generally composed of ornithospherite, dang ornithospherite, serpentine, ornithospherite ornithospherite, monolithospherite ornithospherite, bibiornithospherite ornithospherite, komatiite, etc. Basic rocks are also called mafic rocks, and generally consist of mottled rocks, basaltic rocks, drylights, etc.\|[0068] The basic rock is composed mainly of magnesium silicate (magnesium silicate) and CaSi such as MgSiO3 (olivine) and Mg2SiO4 (olivine). Contains mgSi2O6 (pyroxite), and may also contain a silicated mineral such as CaAl2Si2O8. The magnesium silicate belongs to the group 2, and the mineralization reaction is not so fast.\|[0069] On the other hand, magnesium oxide (MgO) belonging to Group 1 and very fast mineralization reaction (generally considered to be about 0 to 10 mass% in general, but it is not limited to this range) is appropriate for the ultra-basic rock. It is considered that the total amount of the compounds in Group 1 is about 5 to 20 mass%. In addition, it is a natural rock suitable for mineralization because silica (SiO2) and alumina silicate are hardly contained in the suprabasic rock. In addition, ultrafine rocks are natural rocks that are widely available in large quantities.\|[0070] The basic rock is composed mainly of CaAl2Si2O8 and other suitable compounds. and CaMgSi2O6 (pyroxene). Magnesium silicate (magnesium silicate) such as MgSiO3 (talc), Mg2SiO4 (talc), etc. are also included.\|[0071] Rocks containing many amorphous (amorphous) compounds (rocks with a large amount of amorphous phase) have low reactivity and often interfere with mineralization. Since they envelop other crystals and are involved in the amorphous phase, they are connected to each other (it is important to advance the mineralization reaction). (This will prevent you from doing so.\|[0072] In the state of the rock before grinding, the amorphous portion of the rock (the rock having a large amount of an amorphous phase) containing a large amount of an amorphous compound is generally preferred to be 30 mass% or less. If the proportion of amorphous (amorphous) parts is 30 mass% or less, it is considered that completely enclosing the crystals is suppressed, even if the amorphous phase (amorphous part) may occupy the space between the crystalline minerals. The above range includes the presence of other components of the rock (natural rock includes the presence of pulsatile rocks, etc.). Therefore, the range of exposure depends on the particle size (particle size) and the carbon dioxide concentration of the air in contact with the particles.\|[0073] (A-2) Pulverization: In the case of natural rocks, the rock is mined and then pulverized to form fine particles. In the micronization process, the crystal state of each rock-forming compound is maintained (amorphous). (This is important.\|[0074] When the compound constituting the rock is pulverized into fine particles, the smaller the particle size, the larger the surface area of the fine particles and the larger the contact surface with air (carbon dioxide). However, if the particle size is too small, the rock becomes amorphous and the reactivity to mineralization decreases.\|[0075] Of the above compounds, the compounds listed in Table 2 are selected, and the approximate particle size (amorphous diameter) to be amorphous (amorphous diameter) when pulverized into fine particles is listed in Table 2. In addition, "grinding efficiency of each compound" and "effective rate of mineralization" are also listed in Table 2. In addition, the amorphization diameter shown in Table 2 is only a guide, and it does not reliably amorphize if it is below this diameter.\|TABLE 2\|[0076] \|[0077] The time t required for the reaction of the fine particles having a radius of R(m) to reach the depth δ is expressed in formula (III). The concentration of calcium (Ca) and magnesium (Mg) in a solid is ρ, the vapor phase concentration of CO2 is Cg, and the diffusion coefficient of ions through the product layer is D (m2/s).\|[0078] \|[0079] t: Time (sec) ρ: Sum of molar density of magnesium (Mg) and calcium (Ca) in rock (moles/m3-rock) R: Radius of fine particles (m) D: Concentration of CO in the compound Diffusion coefficient of CO2 (m2/s)Cg: CO2 molar concentration in gas phase (moles/m3-gas) δ: Reaction depth (m)\|[0080] On the other hand, if the radius (particle size) of the fine particles is too large, it takes a very long time for all of the fine particles to react, which is also undesirable. According to the unreacted nuclear model, the reaction rate is considered to be inversely proportional to the cube of the diameter of the particles. For example, if the crushing result is 6 μm as a result of assuming 3 μm, the reaction is considered to be 8 (23) times slower.\|[0081] The diffusion coefficient, D, represents the rate of CO2 diffusion through the product layer in the unreacted nuclear model (m2/s), and does not directly represent the mineralization rate of carbon dioxide because of other factors. Since diffusion through the product layer is a rate-limiting step of pneumonialization of CO2, a large diffusion coefficient D actually indicates a mineral that rapidly mineralizes carbon dioxide.\|[0082] The outer diameter (particle size) of the fine particles is determined by the mass of the compound belonging to the above group 1 relative to the total fine particles of the rock obtained. It is considered that the reaction proceeds without crushing the rock more finely than necessary, and that the generation of carbon dioxide by energy loss or crushing can be suppressed, and in addition, the amorphization of the rock (compound) can be suppressed.\|[0083] On the other hand, the reactivity of the whole rock is determined by the type of other components of the rock (natural rock includes the presence of pulsatile rocks, etc.). The composition of the rock may also be referred to as the "rock element", and the composition and composition of the crystalline layer and the amorphous phase, the relationship between the crystalline layer and the amorphous phase, and other factors such as the amount of carbon dioxide oxidation (hereinafter referred to as the "rock element") may also be used. The range of particle size of the crushed rock is also affected by these factors.\|[0084] In view of these facts, when microparticulating rocks, the particle size of the fine particles is generally preferably 100 μm or less (more preferably 50 μm or less, more preferably 25 μm or less, more preferably 10 μm or less. In consideration of the rock elements, appropriate selection may be made, for example, within the range of particle sizes of 1-25 μm, 1-20 μm, 1-10 μm, 1-5 μm, 1-3 μm, etc. For example, when a first group of highly reactive compounds is contained, the particle size may be 1-25 μm (preferably 1-10 μm).\|[0085] If the particle size is 1 to 3 μm, the surface area is large and good reactivity can be expected, but as shown in Table 2, if the particle size is made too small, amorphization may progress and the reactivity may actually become poor. Therefore, it is preferable to limit the particle size of 1 to 3 μm to about 1 to 10 μm or less with the target of 1 to 3 μm. Regarding the particle size of the fine particles, for example, the fine particles of the crushed rock can be spread so as not to overlap, the image acquired by the optical microscope or the like can be analyzed by a computer, and the particle diameter (particle diameter) and shape of the complete distribution of the fine particles can be determined (preferably, the maximum particle diameter is adopted. ). It is desirable that at least 5000 (or 10000) particles are analyzed for each sample of the compound.\|[0086] The rock crushing operation in the micronization can be performed by using a conventionally known crushing means, but, for example, it is preferable to perform the rock by using vertical roller mill, high pressure grinding rolls, etc. It should be noted that ball mills generally have low energy efficiency and tend to become amorphous.\|[0087] In the case of simply atomizing the rock, the rock may be put into a mortar and crushed by using a mortar and a scraper to obtain a desired particle size. In the crushing of rocks by mortar and mortar, for example, it is possible to achieve a very low degree of amorphization by separating very small fine particles that are expected to have been amorphized when they are produced and carrying out a minimum amount of crushing to achieve a desired particle size.\|[0088] Rock crushing prevents amorphization, reduces particle distribution (size distribution of fine particles) as much as possible, minimizes energy consumption (energy consumption generates carbon dioxide, and substantial carbon dioxide reduction is reduced. (3) should be taken into account. These are considered to be particles that have become too small (amorphous) while grinding, for example, using high-pressure grinding. Also, the load of the crusher can be reduced (energy efficiency can be increased) by separating. (This will be retained for the purpose of separation.) On the other hand, the low-pressure grinding (low-pressure grinding) is preferably ground by a vertical roller mill, which is considered to be an aspect of the high-pressure grinding means, because the supplied energy causes dislocation (amorphization) of the crystal structure and generation of heat and sound (energy loss).\|[0089] It is preferable to reduce (narrow) the particle distribution in rock crushing as much as possible. By narrowing the particle distribution, the air to be contacted to mineralize carbon dioxide diffuses into the particulate layer.\|[0090] Such diffusion is an important factor in CO2 mineralization, and it is considered inefficient that the wide particle distribution reduces the porosity between particles, and only the upper part of the ground layer comes into contact with CO2. Less diffusion means that the rock is spread into a thinner layer (the rock layer becomes thinner. It means that it is necessary. The thinning of the rock layer is undesirable because it reduces the amount of rock that can be processed per unit volume of the equipment and at the same time increases the number of sheets per unit rock, which increases the cost.\|[0091] A commercial air classifier or a sieve, etc., may be used for classification. A pulverizer having a classification function may also be used. The particle size distribution is performed by using a conventional technique (for example, measuring the classified fine particles by using an optical microscope equipped with a computer vision operated by commercial software). (You can use it to do this.\|[0092] For example, as also described in CaMgSiO4 in Table 1, there are cases where the compound that has become amorphous as a result of microparticle formation mineralizes CO2 more rapidly than a compound that is not amorphous (crystalline compound). In this case, since the structure of the amorphous compound changes depending on the ratio of the cation to the silica, certain compositions such as CaMgSiO4 favorably react with carbon dioxide even in the case of an amorphous structure and mineralization proceeds.\|[0093] On the other hand, such cases are an exception, and from the point of view of engineering, you will never find pure minerals, and there is always a certain degree of mixing and variation in composition. Therefore, the significant reduction in carbon dioxide mineralization associated with most amorphous compounds outweighs the small performance gains of some compounds. In other words, it is preferable to avoid amorphous compounds because the reaction rate with carbon dioxide and the rate of mineralization are likely to be very low.\|[0094] Further, it is preferable that the rock fine particles obtained by the micronization step are not present as much as possible in the rock fine particles, because the mineralization reaction cannot be expected for the group 4 (compound not expected to react) originally contained in the rock fine particles due to the amorphization of the rock or the amorphization of the rock fine particles together with the micronization. These are preferably about 80 mass% or less in total, and are particularly preferably 50 mass% or less.\|[0095] (B) Carbonate formation process: Fine particles of the rock obtained are brought into contact with air in a predetermined space, whereby carbonates are formed in the fine particles. In other words, carbon dioxide in the air reacts with the fine particles of the rock composed of the above composition, and carbonates (mainly carbonates such as calcium and magnesium) are formed on the surface of the fine particles or in the inside thereof. As a result, carbon dioxide in the air is removed.\|[0096] The space shall be in a state where air is constantly stable (such as stably supplying air containing carbon dioxide and maintaining the conditions described below for the period of implementation, etc.). However, such a stable state can be easily and reliably formed, and it is preferable to use the stone in the room. The space is preferably a closed space capable of supplying air at a certain frequency by ventilation or the like.\|[0097] The introduced air refers to air in general that contains carbon dioxide, for example, the atmosphere (carbon dioxide content is considered to be about 400 to 450 ppm. All gases that are considered to contain carbon dioxide (CO2), such as exhaust gas, can be used. There are also no restrictions on the CO2 concentration of the air in question.\|[0098] The space is conditioned to have a temperature of 15 to 50°C and a relative humidity of 50 to 100%. Both the temperature condition and the humidity condition are within the aforementioned ranges, so that carbon dioxide is mineralized efficiently. The temperature in the space is preferably 20-40°C, and is particularly preferably 30-35°C. The relative humidity is preferably 60-95%.\|[0099] The flow rate of air containing carbon dioxide in a space can be appropriately determined according to the concentration of carbon dioxide, the type and composition of rocks. For example, a natural suprabasic rock (ultrapascular stone) is used as a rock, and the air to be carbon dioxide removed is used as the atmosphere (the carbon dioxide content is at the same level as described above). In this case, it is preferable that the exposure rate be approximately 1 to 100mm/sec, and particularly preferably 1 to 10mm/sec. Since the fine particles of the rock have a small particle diameter and are pulverized, it is preferable to use the above level to prevent the scattering of the fine particles.\|[0100] In the space, the contact between the rock particles and the air is not particularly restricted, but for example, a tray or the like placed in the space may be placed in a container with a shallow bottom such as a tray having an arbitrary area, and spread in a laminar state over the entire bottom surface of the tray.\|[0101] When stratification of rock particles in this way, it is necessary to consider the diffusion of CO2 into the deepest part of the layer. When rocks are crushed to the micrometer level, the diffusion of carbon dioxide in the air spaces between the particles is considered to be due to molecular diffusion. Therefore, there is a concern that the accumulation of fine rock particles in a thick layer decreases the concentration of carbon dioxide at the lower part (deep part) of the fine rock particles and slows the mineralization reaction. On the other hand, the degree of this deep region depends on the type of rock (compound), the size of the space, the particle size of the fine particles, the flow velocity of the air, etc.\|[0102] Based on the above, the thickness of the rock fine particles (fine particle layer) when spread in a layered state is, for example, preferably 5 cm (50 mm) or less, preferably 1-50 mm, more preferably 1-20 mm, more preferably 1-10 mm, and more preferably 1-5 mm.\|[0103] When the fine particles are put in the tray or the like and brought into contact with the air in the state of spreading the tray or the like in a layered state, the tray or the like may be mounted in a multistage in the height direction in the space.\|[0104] The contact time (reaction time) of air and rock particles. However, as a guide, it can be arbitrarily selected as 7 days to 1 year, for example, between 7 days and 2 months. Depending on the amount and type of rocks, the mineralization reaction is considered to have been completed approximately one year after the contact (mineralization reaction) began.\|[0105] When carbonates are formed in the fine particles of rock and carbon dioxide is mineralized, carbonates are accumulated on the surface of the rock, and the mass of fine particles of rock in which a large number of fine particles are assembled is first heated at less than 100°C to remove the adsorbed water. This procedure and the analytical procedures described below are not necessary if the generated carbonate, etc. are not analyzed.\|[0106] After the water is removed, the amount of mineralized carbon dioxide can be confirmed by comparing the mass change with the mass of the fine particles of the rock before the carbonate formation process as an analytical operation. In addition, carbon dioxide mineralized by thermogravimetric differential thermal analysis (TG-DTA) and X-ray fluorescence analysis (XRF) can be analyzed in detail such as the amount of carbon dioxide (carbonate).\|[0107] In addition, environmentally-harmless carbonates (mainly calcium and magnesium carbonate such as calcium carbonate (CaCO3 and MgCO3). The mineralized rocks can be used, for example, as subbase materials or construction materials for landfill. Thus, the mineralized rocks are environmentally friendly.\|[0108] (C) Effect of the present invention: The present invention is such that carbon dioxide in the air is mineralized as a carbonate by micronizing rocks containing alkaline earth metals and bringing the obtained microparticles into contact with air in a space having a predetermined environment, thereby fixing carbon dioxide to the rocks and removing carbon dioxide in the air.\|[0109] Consequently, the present invention can easily remove carbon dioxide from the air at low cost without using a chemical or using a large-scale facility, etc., and can substantially reduce carbon dioxide because the amount of carbon dioxide generated is small. In addition, there is no need of storing carbon dioxide, and there is no risk in such storage, and the immobilized carbon dioxide becomes a carbonate harmless to the environment, and can be reused together with rocks, so that it is also environmentally friendly.\|[0110] According to the present invention, CDR. can be performed without relying on other technologies and infrastructure. Conventional technologies require a large amount of energy to remove carbon dioxide from the air, and considering the carbon dioxide generated by such energy, many of the technologies have not reduced carbon dioxide substantially. On the other hand, the present invention removes carbon dioxide from the air by a simple method, i.e., a step for atomizing rocks and a step for forming a carbonate by reacting the obtained rock particulates with carbon dioxide in the air. Therefore, the present invention is considered to be a technology that requires less energy and leads to a substantial reduction in carbon dioxide.\|[0111] There are currently two main types of CDRs. These are Bioenergy with Carbon Capture and Storage (BECCS) with carbon dioxide (CO2) recovery and storage, and direct air recovery with carbon dioxide storage (DIRECT Air CO2 Capture with Storage:DACCS).\|[0112] Of these, BECCS relies on biomass combustion, carbon dioxide capture, transport to storage sites, and underground storage. The DACCS also uses machinery to filter carbon dioxide from the air before transport and underground storage. The main points to compare are energy requirements (GJ/t-CO2), land requirements (km2/Mt-CO2), water requirements (m3/t-CO2), the time required for CO2 recovery, biological restrictions (Gt-CO2/year), and cost. In all of these cases, t-CO2 means net carbon dioxide (CO2) removed from the environment (accounting for carbon dioxide emissions from processes and supply chains). ). Table 3 shows the comparison of the present invention and these two technologies. Table 3 confirms that the present invention works more advantageously than other technologies.\|TABLE 3\|[0113] \|[0114] In addition, there are scale-up and scale-out ratio issues. BECCS and DACCS usually limit their use to very large (>1Mt-CO2/year) reservoirs because they require reservoirs and transport infrastructure, and development of reservoirs is costly. On the other hand, the present invention can be applied at any scale, whether in the kg scale or in the Mt scale. Therefore, it is considered that small, medium and large-scale systems can be developed without worrying about transportation, storage, etc.\|[0115] In addition, it is not possible to accurately quantify the amount of CO2 removed by other methods using soil and oceans, and there is also the problem that such other methods may lose future CO2 expected due to the impact of climate change. Since carbon dioxide is immobilized as a carbonate by the above simple means and removed from the air, these problems can also be solved.\|[0116] (D) Variations of embodiments: The embodiments described above represent one aspect of the present invention, and the present invention is not limited to the aforementioned embodiments. Needless to say, the content of the present invention includes variations and improvements provided in the configuration of the present invention and to the extent that the purpose and effects can be achieved. The specific structure, shape, etc. in implementing the present invention are acceptable as other structures, shapes, etc., to the extent that the purpose and effect of the present invention can be achieved. The present invention is not limited to each of the embodiments described above, and any deformation or improvement within the scope of achieving the purpose of the present invention is included in the present invention.\|[0117] For example, although necessary operations for (A) the micronization step and (B) the carbonate formation step are partially illustrated, there is no problem with using other procedures not illustrated, to the extent that they do not interfere with the purpose and effect of the present invention. Similarly, a compound capable of constituting a rock is listed as an example, but since it is only an example, there is no problem in including other compounds in the rock used in the present invention, such as a compound containing an alkaline earth metal. Other specific structures, shapes, etc., in the implementation of the present invention may be other structures, etc., to the extent that the purpose of the present invention can be achieved.\|EMBODIMENTS EXAMPLE\|[0118] The present invention is described in more detail below based on examples, etc., but the present invention is not limited to these.\|[0119] (Reference Example 1, Examples 2 to 6, Reference Example 7, Example 8) The composition shown in Table 4 below (Analytical Means of Compound Composition, etc. are described below as equivalent to rock. 8 types of slag (Example 1 to Example 8 (Example 1, Example 2 to Example 6, Example 7, and Example 8) (Prepared). In addition, "%" indicates the content (mass%) to the whole.\|[0120] (Composition of Slag)\|TABLE 4\|[0121] Slag 1 to slag 8 were ground using a mortar and a scraper, and the ground slag was classified using a sieve. The particle size distribution of the slag particles after classification was measured using an optical microscope equipped with a computer vision operated by "ImageJ" software, which is one of the image processing techniques, and a particle sample with a particle size of 25-90 μm and a particle sample with a particle size of less than 25 μm were obtained respectively. In addition, the elemental compositions of slag (1-8) and the compound compositions of slag (1-8) were analyzed by XRF and Q-XRD, respectively (the compound compositions, etc. are shown in Table 4. ).\|[0122] The obtained fine particle samples were placed in a circular tray of 10cm diameter x 1 cm height respectively, and spread so that the thickness becomes 3 mm.\|[0123] The indoor space of a 22L-volume incubator (3-6815-01 CO2 incubator: made by Azwan Co., Ltd.) was set to have a relative humidity of 90% and a temperature of 30°C. Under such a humidity and temperature, a tray containing a particulate sample is placed in the indoor space of the incubator, the door is closed and sealed, and then air having a carbon dioxide concentration of 5% (slag 1-slag 5) and air having a carbon dioxide concentration of 20% (slag 5-slag 8) are introduced. Air was brought into contact with the particulate samples to mineralize carbon dioxide (form carbonate) so as to maintain this state. The test was performed on 1, 3, 7, 14, 21, and 28 days after the start of study treatment. ). Each sample was tested 3 times (n = 3) (Table 5 shows the mean values. ).\|[0124] After the number of days had elapsed, the particulate samples were measured in mass and carbon dioxide (carbonate) mineralized by thermogravimetric differential thermal analysis (TG-DTA) and X-ray fluorescence analysis (XRF) were analyzed. Table 5 and Table 6 show the mineralization ratio (%) of carbon dioxide corresponding to the number of days elapsed (the experimental value is Table 5, but the predicted value is listed in Table 6 as a reference. ). Two carbon dioxide concentrations were evaluated to confirm the unreacted nuclear model.\|TABLE 5\|[0125] \|TABLE 6\|[0126] \|[0127] From the results of Table 5, firstly, the mineralization ratio of slag 1 and slag 7 is very low (for example, 1% or less under the conducted carbon dioxide concentration conditions (slag 1 is 28 days old, slag 7 is 7 days old). ) can be confirmed. The reason for this is that both slag 1 and slag 7 are originally amorphous phases (amorphous parts). The same applies hereinafter. It is considered that the slag 1 and the slag 7 contain 34.1% and 100%, respectively. Since all (100%) of the slag 7 is an amorphous phase, the mineralization ratio is considered to be low.\|[0128] In the case of the slag (1), on the other hand, the amorphous phase accounts for 34.1% of the total amount, but the amorphous phase still accounts for a high percentage of the total amount. Therefore, crystals are trapped in the amorphous phase, and the crystals are not connected to each other, and only the crystals on the surface react, and therefore the mineralization ratio is considered to be low.\|[0129] Generally, when molten rock (natural rock or slag) is cooled, crystalline or amorphous compounds are formed, but rapid cooling tends to produce amorphous compounds, and slow cooling tends to produce crystals. The distribution of nucleation crystals in molten rock is random, and these crystals grow until they come into contact with other crystals. On the other hand, in the liquid phase between the crystals, if the crystals have solidified as an amorphous phase before growing together, the crystals are separated from each other and cannot be connected. Such an arrangement would hinder the progress of the mineralization of carbon dioxide.\|[0130] In addition, slag 1 and slags other than slag 7 (slags 2 to 6, slags 8) also contained an appropriate amount of amorphous phase. The above behavior was not observed, and the results in Table 5 confirmed that mineralization also progressed well (for example, mineralization rate is 5% or more when the number of days elapsed is 7 under the conducted carbon dioxide concentration conditions. ). This is probably because the amorphous phase occupied the space between the crystalline minerals but did not completely envelop the crystals.\|[0131] The slag (slag 2, slag 4, slag 6, and slag 8) containing a compound such as calcium oxide (oxide) belonging to the group 1 shows mineralization of carbon dioxide at an initial stage. In particular, the rapid mineralization of slag 2 and slag 4 is characterized by the calcium content mainly in oxide form (CaO and Ca2Fe2O5) and calcium silicate (both belong to Group 1). It is considered to be caused by the above.\|[0132] On the other hand, the mineralization ratio of the slag 3 and the slag 5 is relatively lower than that of the slag 3 and the slag 5, because the mixed cation silicate belonging to the group 2 is substituted with Mg or Fe to some extent. It is also considered that there are compounds belonging to Group 4.\|INDUSTRIAL APPLICABILITY\|[0133] The present invention can be advantageously used as a means for providing a technique that enables carbon dioxide in the air to be immobilized as a carbonate on a rock to reduce carbon dioxide in the air, and has high industrial applicability.	Family Number\|(102507569)\|102507569\|Advantages / Prev. Drawbacks\|(JP2022169854 A)\|Accordingly, the present invention enables the easy removal of carbon dioxide from the air at low cost without the use of any chemical or without the use of any large-scale equipment or the like, and also enables the substantial reduction of carbon dioxide because of the reduced amount of carbon dioxide to be (...) \|Moreover, the method disclosed in non-patent document 3 is a method of simply dispersing crushed rock on the soil surface, but it was not preferable because it is difficult to estimate the mineralization amount of carbon dioxide and it can adversely affect the environment.\|	Chemical engineering\|Environmental technology	Y02C-020/40		Y02C-020/40	B01D-053/14\|B01J-020/02\|B01J-020/04\|B01J-020/06\|B01J-020/08\|B01J-020/10	B01D-053/14\|B01J-020/02\|B01J-020/04\|B01J-020/06\|B01J-020/08\|B01J-020/10			WO202604248\|JP2026006164\|JP2025117160	WO202604248 117257809 WHO=Examiner SELF=N CAT=Y\|JP2026006164 117257809 WHO=Applicant SELF=N\|JP2025117160 115628521 WHO=Applicant SELF=N	JP2000197810\|JP05212278\|JP2017109198\|JP2013504424\|JP03267120	JP2000197810 4041187 WHO=Examiner SELF=N CAT=Y\|JP05212278 13973977 WHO=Examiner SELF=N CAT=X CAT=Y\|JP2017109198 76580681 WHO=Examiner SELF=N\|JP2013504424 46598940 WHO=Applicant SELF=N\|JP03267120 28031985 WHO=Examiner SELF=N	特表２０１３－５０４４２４号公報\|Ｎｄｕａｇｕ，Ｅ．，Ｂｅｒｇｅｒｓｏｎ，Ｊ．ａｎｄＺｅｖｅｎｈｏｖｅｎ，Ｒ．，２０１２．ＬｉｆｅｃｙｃｌｅａｓｓｅｓｓｍｅｎｔｏｆＣＯ２ｓｅｑｕｅｓｔｒａｔｉｏｎｉｎｍａｇｎｅｓｉｕｍｓｉｌｉｃａｔｅｒｏｃｋＡｃｏｍｐａｒａｔｉｖｅｓｔｕｄｙ．ＥｎｅｒｇｙＣｏｎｖｅｒｓｉｏｎａｎｄＭａｎａｇｅｍｅｎｔ，５５，ｐｐ．１１６－１２６．\|Ｎｃｏｎｇｗａｎｅ，Ｍ．ｓ．，Ｂｒｏａｄｈｕｒｓｔ，Ｊ．Ｌ．ａｎｄＰｅｔｅｒｓｅｎ，Ｊ．，２０１８．ＡｓｓｅｓｓｍｅｎｔｏｆｔｈｅｐｏｔｅｎｔｉａｌｃａｒｂｏｎｆｏｏｔｐｒｉｎｔｏｆｅｎｇｉｎｅｅｒｅｄｐｒｏｃｅｓｓｅｓｆｗｏｒｔｈｅｍｉｎｅｒａｌｃａｒｂｏｎａｔｉｏｎｏｆＰＧＭｔａｉｌｉｎｇｓ．ＩｎｔｅｒｎａｔｉｏｎａｌＪｏｕｒｎａｌｏｆＧｒｅｅｎｈｏｕｓｅＧａｓＣｏｎｔｒｏｌ，７７，ｐｐ．７０－８１．\|Ｋｅｌｌｅｒ，ｄ．Ｐ．，Ｌｅｎｔｏｎ，Ａ．，Ｌｉｔｔｌｅｔｏｎ，Ｅ．ｗ．，Ｏｓｃｈｌｉｅｓ，Ａ．，Ｓｃｏｔｔ，ｖ．ａｎｄＶａｕｇｈａｎ，Ｎ．Ｅ．，２０１８．Ｔｈｅｅｆｆｅｃｔｓｏｆｃａｒｂｏｎｄｉｏｘｉｄｅｒｅｍｏｖａｌｏｎｔｈｅｃａｒｂｏｎｃｙｃｌｅ．Ｃｕｒｒｅｎｔｃｌｉｍａｔｅｃｈａｎｇｅｒｅｐｏｒｔｓ，４（３），ｐｐ．２５０－２６５．	JP05212278; JP2000197810; JP03267120; JP2017109198; 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date=2025-06-13\|Event code=JP/A61\|Event indicator=Pos\|Event group=Event indicating In Force\|First payment of annual fees (during grant procedure)\|Japanese intermediate code: A61\|Effective date of the event=2025-06-11\|Event publication date=2025-06-25\|Event code=JP/R150\|Event indicator=Pos\|Event group=Event indicating In Force\|CERTIFICATE OF PATENT OR REGISTRATION OF UTILITY MODEL\|Japanese intermediate code: R150\|Event publication date=2025-06-30\|Event code=JP/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Published granted patent (Second level) from 01-03-1996 onwards (Published examined patent application (Second level) 1971-1996)\|Publication country=JP\|Publication number=JP7699796\|Publication stage code=B2\|Publication date=2025-06-30\|Standardized publication number=JP7699796		(JP7699796)\|JP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=e5gOkjdPC53qKdruKCQZdjeISh8T7V+NNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=JP0000000022803773&ekey=2281&xpn=JP7699796&kind=B2	https://www.j-platpat.inpit.go.jp/c1801/PU/JP-2021-075533/10/en	https://permalink.orbit.com/RenderStaticFirstPage?XPN=PBN44GkNLeTWqxLm4QBXD3fDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	JP				(JP7699796)\|NAME=HATA, Masanori , REG=100115842\|(JP2022169854)\|NAME=HATA, Masanori , REG=100115842		(JP7699796)\|NAME=Myers, Corey Adam\|NAME=NAKAGAKI Takao\|(JP2022169854)\|NAME=COREY ADAM MYERS\|NAME=NAKAGAKI TAKAO	(JP7699796)\|2	1	1					(JP7699796)\|Number of Claims: NCL=4\|Form: FORM=OL\|Request for examination: REQEXA=false\|Primary examiner: 駒木亮一\|\|(JP2022169854)\|Number of Claims: NCL=7\|Form: FORM=OL\|Request for examination: REQEXA=false\|Primary examiner: 駒木亮一\|	(JP7699796)\|Previous publication: JP2022169854 2022-11-10 [JP2022169854]	(JP7699796)\|JAPANESE (JPN)	(JP7699796)\|Patent\|(JP2022169854)\|Patent	Titre: (JP7699796)\|How to remove carbon dioxide from the air Résumé: (JP7699796)\|PROBLEM TO BE SOLVED: To provide a method which can be executed at low cost, can substantially reduce carbon dioxide, and removes carbon dioxide in the air friendly to an environment with no risk of storing the carbon dioxide.SOLUTION: The present invention atomizes a rock containing an alkaline earth metal, immobilizes carbon dioxide to the rock by bringing acquired fine particles into contact with the air in a space as prescribed environment to mineralize carbon dioxide in the air as carbonate, and removes the carbon dioxide in the air. The invention can easily remove the carbon dioxide in the air at low cost without using chemical, and can remove qualitative carbon dioxide with little production amount of accompanying carbon dioxide. In addition, the immobilized carbon dioxide becomes carbonate harmless to environment and friendly to the environment with no risk of storing the carbon dioxide.SELECTED DRAWING: Figure 1COPYRIGHT: (C)2023,JPO&INPIT	44	Abstract	gpt-4o-mini	yes	The patent describes a method for mineralizing CO₂ using alkaline earth metal-containing rocks, which aligns with the goal of enhanced weathering and carbon sequestration.
45	EP12306468	EP12306468	EP2735553\|EP2735553	66070146	EP2735553 B1 2017-04-05 [EP2735553]\|EP2735553 A1 2014-05-28 [EP2735553]	2012-11-27	2012-11-27	2017-04-05\|2014-05-28	(EP2735553)\|2017-04-05	(EP2735553)\|2020-10-30	(EP2735553)\|Process for the treatment of a silicate mineral	(EP2735553)\|The invention provides a process for the preparation of a first product comprising an alkali metal magnesium orthosilicate and (i) magnesium oxide or (ii) an alkali metal silicate, which process comprises the reaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R 2 O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO 2 , being from 4:1 to 1:4, and contacting the first product with water to produce a second product comprising magnesium hydroxide and isolating or producing further useful products from the second product.	LAFARGE	(EP2735553)\|LAFARGE ([FR])\|(EP2735553)\|LAFARGE ([FR])	GARTNER ELLIS\|PISCH ALEXANDER\|MEYER VINCENT	(EP2735553)\|Gartner, Ellis\|Pisch, Alexander\|Meyer, Vincent\|(EP2735553)\|Gartner, Ellis\|Pisch, Alexander\|Meyer, Vincent	(EP2735553)\|Keschmann, Marc;Haffner und Keschmann ([AT])\|Reg. Nb: 101393339	(EP2735553)\|However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible.\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled.\|Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300°C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eiteleite, Na2CO3*MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|	(EP2735553)\|1. A process for the treatment of a silicate mineral comprising: - a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate and a magnesium oxide, which step comprising the reaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula F2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, - a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate,and - a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product\|	(EP2735553)\|The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|The present invention accordingly provides a process for the treatment of a silicate mineral comprising a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate of the general formula R2MgSiO4 wherein R represents an alkali metal, and magnesium oxide which process comprises the reaction, at a temperature from 500 to 200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate, and a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product.\|This invention relates to a process for the treatment of a silicate mineral, The process uses as starting material a magnesium silicate and produces an alkali metal magnesium orthosilicate and magnesium oxide each of which can be isolated or subjected to further treatment to produce other products.\|	(EP2735553)\|SILICATE MINERAL(100,4)\|SILICATE MINERAL TREATMENT(100,4)\|MAGNESIA(97,20)\|MAGNESIUM ORTHOSILICATE(89,16)\|AMORPHOUS SILICA PRECIPITATE(79,2)\|MAGNESIUM SILICATE(72,49)\|SILICA PRECIPITATE(70,1)\|OUTGOING HOT GAS(64,1)\|MOVING GRATE FURNACE(62,2)\|MAGNESIUM OXIDE(58,25)\|OUTGOING HOT SOLID(58,1)\|ALKALI METAL CARBONATE(56,49)\|PRODUCT CARBONATION(56,4)\|MOLAR RATIO(53,10)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(50,11)\|NEUTRALIZING(50,1)\|ALKALI METAL(48,75)\|EITELEITE(48,1)\|INCOMING SOLID(48,1)\|IRON ISOLATION(48,1)\|ALKALI METAL DISSOLUTION(46,3)\|ALKALI METAL BICARBONATE(44,4)\|FURNACE(42,8)\|NA2CO(40,1)\|MOVING GRATE(38,5)\|INCOMING COMBUSTION AIR(38,1)\|NET ENERGY CONSUMPTION(36,2)\|USEFUL PRODUCT(36,2)\|TEMPERATURE ELEVATION(36,1)\|METHANEDIONE(35,5)\|COUNTERCURRENT HEAT EXCHANGE(35,3)\|CHROMIUM COMPOUND(35,2)\|PELLET(29,16)\|AMBIENT TEMPERATURE(28,2)\|MAGNESIUM OXIDE MOLAR RATIO(28,1)\|CO2(27,22)\|DEHYDRATION(26,2)\|UNREACTED OLIVINE(24,3)\|COMPLEX ALKALI METAL(24,1)\|MGCO(23,8)\|BED(23,5)\|HEAT EXCHANGE(22,4)\|PREHEATER CYCLONE TOWER(22,1)\|ALKALI METAL SILICATE(21,7)\|LAB FURNACE(20,4)\|OLIVINE SAND(20,3)\|PLATINUM CRUCIBLE(20,3)\|PHOTOMETRY HYDROMAGNESITE MG(20,1)\|SOLID PRODUCT(19,11)\|XRF SPECTROMETRY(19,2)\|GASEOUS CO2(18,4)\|ASBESTOS FIBRILLAR(18,1)\|DECARBONATED NODULE(18,1)\|OBSCURATION STABILIZATION(18,1)\|HYDRAULIC BINDER(17,3)\|HYDROMAGNE SITE(17,3)\|FINE SUSPENSION(16,4)\|EARTH CRUST(16,2)\|LASER GRANULOMETRY(16,2)\|RESIDUAL R2CO(16,2)\|CENTRATE TAILING(16,1)\|COUNTER CURRENT HEAT EXCHANGE(16,1)\|DECARBONATED PELLET(16,1)\|METHANEDIONE GAS LIBERATION(16,1)\|ANHYDROUS MAGNESIUM SILICATE(14,2)\|SI CA MG(14,2)\|ABSORB METHANEDIONE(14,1)\|CO2 NET CONSUMER(14,1)\|CO2 SEQUESTRATION(14,1)\|DISSOLUTION BEHAVIOR(14,1)\|HEAT TRANSFER(14,1)\|HELICOIDAL TEFLON(14,1)\|MAGNETITE TRACE(14,1)\|METHANEDIONE EVAPORATION(14,1)\|MINIATURE FLOTATION CELL(14,1)\|PREHEATER TOWER(14,1)\|SILICATE HYDROPHOBICITY(14,1)\|ANHYDROUS PRODUCT(13,5)\|ARTINITE(13,5)\|AUTOCLAVE(13,5)\|FILTER CAKE DRYING(13,5)\|FORSTERITE(13,4)\|ENERGY EFFICIENCY(13,3)\|SAMPLE REACTION(13,3)\|FE2O(12,9)\|EITELITE(12,4)\|MG2SIO(12,4)\|NA2MGSIO(12,4)\|PARTICULATE(12,4)\|POWDERED PRODUCT(12,4)\|PRODUCT RICH(12,4)\|BURNING ZONE(12,2)\|TRANSITION METAL(12,2)\|CARBONATE PARTICLE(12,1)\|CONCENTRATE CO2 CONTENT(12,1)\|ENHANCE NA RECYCLING(12,1)\|EXPERIMENT MULTIPLIER(12,1)\|GROUND OLIVINE MIX(12,1)\|LASER GRANULOMETER(12,1)\|NODULE RISK(12,1)\|PERFECTLY BALANCED EQUATION(12,1)\|PRINCIPAL DISSOLVED ANION(12,1)\|PRODUCT HECTORITE MANUFACTURER(12,1)\|SAMPLE DEAGGLOMERATION(12,1)\|SUSPENSION PREHEATER(12,1)\|UNREACTED ANHYDROUS COMPOUND(12,1)\|UNTREATED RESIDUE(12,1)\|COLORLESS SOLUTION(11,2)\|ESTIMATED MG(11,2)\|GAS ANALYZER(11,2)\|MAGNESIUM OXIDE HYDRATION(11,2)\|REACTED SAMPLE PHASE CONSTITUTION(11,2)\|REACTION PRODUCT(10,7)\|ALKALI METAL OXIDE(10,6)\|ALKALINE SOLUTION(10,3)\|COMBUSTION EXHAUST GAS(10,3)\|HYDROCYCLONE(10,3)\|NESQUEHONITE(10,3)\|PERICLASE(10,3)\|QUENCHING(10,3)\|AMORPHOUS MAGNESIUM SILICATE(10,1)\|CO2 EMISSION(10,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(10,1)\|DECARBONATION REACTION(10,1)\|EARTH MANTLE COMPONENT(10,1)\|FERMENTATION RESIDUE GAS(10,1)\|FINE NESS(10,1)\|FINE SAND GRANULOMETRY(10,1)\|FLOTATION AID(10,1)\|INORGANIC IMPURITY(10,1)\|LAYERED DOUBLE HYDROXIDE(10,1)\|MINERAL CARBONATE(10,1)\|MOVING GRATE COOLER(10,1)\|OLIVINE SAMPLE(10,1)\|PRECIPITATED SILICA(10,1)\|R2O MOLAR RATIO(10,1)\|RAW MAGNESIUM SILICATE(10,1)\|ROCK SPECIES(10,1)\|SLURRY CONC(10,1)\|SODIUM SILICATE MILIMOLE LITER(10,1)\|SUSPENSION AGITATION(10,1)\|SYNTHETIC HECTORITE(10,1)\|UNREACTED MAGNESIUM SILICATE(10,1)\|UNREACTED PARTICLE(10,1)\|VESSEL PRESSURIZATION(10,1)\|WORKING SESSION(10,1)\|NA2O(9,4)\|CARBOXYMETHYLCELLULOSE(9,3)\|MAGNESIUM SILICATE WATER(8,5)\|SODIUM OLEATE(8,5)\|CEMENT PLANT(8,4)\|HOT GAS(8,4)\|R2SIO(8,4)\|ROTARY KILN(8,4)\|ACTINOLITE(8,2)\|AMOSITE(8,2)\|AMPHIBOLE(8,2)\|ANHYDROUS SODIUM CARBONATE(8,2)\|BRUCITE(8,2)\|CENTRIFUGATION(8,2)\|CHRYSOTILE(8,2)\|COMPLEX MAGNESIUM(8,2)\|CRYSTALLINE PHASE(8,2)\|ENSTATITE(8,2)\|FILTER CAKE MG(8,2)\|LIQUID FILTRATE(8,2)\|MEASURED LOI DATA(8,2)\|MG CONTENT(8,2)\|MGO SILICA MOLAR RATIO(8,2)\|MIXED POWDER(8,2)\|MR2MGSIO(8,2)\|PYROXENE(8,2)\|SIEVING(8,2)\|SODIUM CARBONATE POWDER(8,2)\|SYMBOL(8,2)\|TREMOLITE(8,2)\|ULTRASOUND(8,2)\|ALKALI BICARBONATE SOLUTION(8,1)\|ALKALI MAGNESIUM METAL ORTHOSILICATE(8,1)\|ALKALI SOLUBLE IMPURITY(8,1)\|BASIC MAGNESIUM ORTHOSILICATE(8,1)\|BIOMASS DERIVED FUEL(8,1)\|BLUE DIODE(8,1)\|CALCULATION MATRIX(8,1)\|CARBONATABLE SOLID(8,1)\|CARBONATE ION(8,1)\|CARBONATED PRODUCT(8,1)\|CHROMIUM CONTENT(8,1)\|CO2 GRAM(8,1)\|COARSE UNREACTED SOLID(8,1)\|COMBINED CO2 QUANTITATIVE DETECTION(8,1)\|COOLED PELLET(8,1)\|CRUSHED SAMPLE(8,1)\|HOT NODULE HEAT(8,1)\|HOT QUENCHED SOLID(8,1)\|INCOMING COMBUSTION AIR PREHEATER(8,1)\|MAGNESIA FINE PARTICLE(8,1)\|MAGNESIUM SILICATE MINERAL(8,1)\|MAJOR IMPURITY(8,1)\|MAXIMUM CO2 CAPTURE(8,1)\|MAXIMUM SLURRY ADDITIVE(8,1)\|NATURAL TALC(8,1)\|NATURALLY OCCURRING MINERAL(8,1)\|OUTGOING SOLID PARTICLE(8,1)\|PHASE PROBABILITY(8,1)\|PLUS MAGNESIUM(8,1)\|POROUS BED(8,1)\|POWDER SELF NODULIZE(8,1)\|PREHEATER TOP CYCLONE(8,1)\|QUALITATIVE PHASE(8,1)\|QUICK WASH(8,1)\|REACTION ESCAPE(8,1)\|REACTOR CONTENT(8,1)\|RED HE NE LASER(8,1)\|SESQUIHYDRATE(8,1)\|SILICA MOLE(8,1)\|SODIUM HYDROXIDE MILLIMOLE LITER(8,1)\|SOLUBLE SALT(8,1)\|SORT REACTION(8,1)\|STEEL CRUCIBLE(8,1)\|SULFUR CONTENT(8,1)\|TABLE EXPERIMENT(8,1)\|TREATED PELLET(8,1)\|TREATED SLURRY(8,1)\|WEAK PEAK(8,1)\|XRD DATA RIETVELD ANALYSIS(8,1)\|METHYL ISOBUTYL CARBINOL(7,5)\|NAFEO(7,2)\|SIEVE(7,2)\|DEIONIZED WATER(6,4)\|ATMOSPHERE PRESSURE(6,3)\|FE3O(6,3)\|H2SIO(6,3)\|HYDROXY CARBONATE WATER(6,3)\|USEFUL PRODUCT STREAM(6,3)\|XH2O(6,3)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|AIR BUBBLING(6,1)\|ALKALINE AQUEOUS SOLUTION(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANTHOPHYLLITE(6,1)\|ANTIGORITE(6,1)\|AQUEOUS ACID(6,1)\|AQUEOUS PHASE ICP ANALYSIS(6,1)\|ARLTHOPHYLLITE(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|CALCINATION(6,1)\|CAO SILICA MOLAR RATIO(6,1)\|CARBONATE PRODUCT(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|CRYSTALLINE PRODUCT(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|DURATIO N(6,1)\|EXCESS FERROUS SULFATE(6,1)\|FAYALITE(6,1)\|FE2SIO(6,1)\|\|(EP2735553)\|SILICATE MINERAL(100,4)\|SILICATE MINERAL TREATMENT(100,4)\|MAGNESIA(97,20)\|MAGNESIUM ORTHOSILICATE(89,16)\|AMORPHOUS SILICA PRECIPITATE(79,2)\|MAGNESIUM SILICATE(72,49)\|SILICA PRECIPITATE(70,1)\|OUTGOING HOT GAS(64,1)\|MOVING GRATE FURNACE(62,2)\|MAGNESIUM OXIDE(58,25)\|OUTGOING HOT SOLID(58,1)\|ALKALI METAL CARBONATE(56,49)\|PRODUCT CARBONATION(56,4)\|MOLAR RATIO(53,10)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(50,11)\|NEUTRALIZING(50,1)\|ALKALI METAL(48,75)\|EITELEITE(48,1)\|INCOMING SOLID(48,1)\|IRON ISOLATION(48,1)\|ALKALI METAL DISSOLUTION(46,3)\|ALKALI METAL BICARBONATE(44,4)\|FURNACE(42,8)\|NA2CO(40,1)\|MOVING GRATE(38,5)\|INCOMING COMBUSTION AIR(38,1)\|NET ENERGY CONSUMPTION(36,2)\|USEFUL PRODUCT(36,2)\|TEMPERATURE ELEVATION(36,1)\|METHANEDIONE(35,5)\|COUNTERCURRENT HEAT EXCHANGE(35,3)\|CHROMIUM COMPOUND(35,2)\|PELLET(29,16)\|AMBIENT TEMPERATURE(28,2)\|MAGNESIUM OXIDE MOLAR RATIO(28,1)\|CO2(27,22)\|DEHYDRATION(26,2)\|UNREACTED OLIVINE(24,3)\|COMPLEX ALKALI METAL(24,1)\|MGCO(23,8)\|BED(23,5)\|HEAT EXCHANGE(22,4)\|PREHEATER CYCLONE TOWER(22,1)\|ALKALI METAL SILICATE(21,7)\|LAB FURNACE(20,4)\|OLIVINE SAND(20,3)\|PLATINUM CRUCIBLE(20,3)\|PHOTOMETRY HYDROMAGNESITE MG(20,1)\|SOLID PRODUCT(19,11)\|XRF SPECTROMETRY(19,2)\|GASEOUS CO2(18,4)\|ASBESTOS FIBRILLAR(18,1)\|DECARBONATED NODULE(18,1)\|OBSCURATION STABILIZATION(18,1)\|HYDRAULIC BINDER(17,3)\|HYDROMAGNE SITE(17,3)\|FINE SUSPENSION(16,4)\|EARTH CRUST(16,2)\|LASER GRANULOMETRY(16,2)\|RESIDUAL R2CO(16,2)\|CENTRATE TAILING(16,1)\|COUNTER CURRENT HEAT EXCHANGE(16,1)\|DECARBONATED PELLET(16,1)\|METHANEDIONE GAS LIBERATION(16,1)\|ANHYDROUS MAGNESIUM SILICATE(14,2)\|SI CA MG(14,2)\|ABSORB METHANEDIONE(14,1)\|CO2 NET CONSUMER(14,1)\|CO2 SEQUESTRATION(14,1)\|DISSOLUTION BEHAVIOR(14,1)\|HEAT TRANSFER(14,1)\|HELICOIDAL TEFLON(14,1)\|MAGNETITE TRACE(14,1)\|METHANEDIONE EVAPORATION(14,1)\|MINIATURE FLOTATION CELL(14,1)\|PREHEATER TOWER(14,1)\|SILICATE HYDROPHOBICITY(14,1)\|ANHYDROUS PRODUCT(13,5)\|ARTINITE(13,5)\|AUTOCLAVE(13,5)\|FILTER CAKE DRYING(13,5)\|FORSTERITE(13,4)\|ENERGY EFFICIENCY(13,3)\|SAMPLE REACTION(13,3)\|FE2O(12,9)\|EITELITE(12,4)\|MG2SIO(12,4)\|NA2MGSIO(12,4)\|PARTICULATE(12,4)\|POWDERED PRODUCT(12,4)\|PRODUCT RICH(12,4)\|BURNING ZONE(12,2)\|TRANSITION METAL(12,2)\|CARBONATE PARTICLE(12,1)\|CONCENTRATE CO2 CONTENT(12,1)\|ENHANCE NA RECYCLING(12,1)\|EXPERIMENT MULTIPLIER(12,1)\|GROUND OLIVINE MIX(12,1)\|LASER GRANULOMETER(12,1)\|NODULE RISK(12,1)\|PERFECTLY BALANCED EQUATION(12,1)\|PRINCIPAL DISSOLVED ANION(12,1)\|PRODUCT HECTORITE MANUFACTURER(12,1)\|SAMPLE DEAGGLOMERATION(12,1)\|SUSPENSION PREHEATER(12,1)\|UNREACTED ANHYDROUS COMPOUND(12,1)\|UNTREATED RESIDUE(12,1)\|COLORLESS SOLUTION(11,2)\|ESTIMATED MG(11,2)\|GAS ANALYZER(11,2)\|MAGNESIUM OXIDE HYDRATION(11,2)\|REACTED SAMPLE PHASE CONSTITUTION(11,2)\|REACTION PRODUCT(10,7)\|ALKALI METAL OXIDE(10,6)\|ALKALINE SOLUTION(10,3)\|COMBUSTION EXHAUST GAS(10,3)\|HYDROCYCLONE(10,3)\|NESQUEHONITE(10,3)\|PERICLASE(10,3)\|QUENCHING(10,3)\|AMORPHOUS MAGNESIUM SILICATE(10,1)\|CO2 EMISSION(10,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(10,1)\|DECARBONATION REACTION(10,1)\|EARTH MANTLE COMPONENT(10,1)\|FERMENTATION RESIDUE GAS(10,1)\|FINE NESS(10,1)\|FINE SAND GRANULOMETRY(10,1)\|FLOTATION AID(10,1)\|INORGANIC IMPURITY(10,1)\|LAYERED DOUBLE HYDROXIDE(10,1)\|MINERAL CARBONATE(10,1)\|MOVING GRATE COOLER(10,1)\|OLIVINE SAMPLE(10,1)\|PRECIPITATED SILICA(10,1)\|R2O MOLAR RATIO(10,1)\|RAW MAGNESIUM SILICATE(10,1)\|ROCK SPECIES(10,1)\|SLURRY CONC(10,1)\|SODIUM SILICATE MILIMOLE LITER(10,1)\|SUSPENSION AGITATION(10,1)\|SYNTHETIC HECTORITE(10,1)\|UNREACTED MAGNESIUM SILICATE(10,1)\|UNREACTED PARTICLE(10,1)\|VESSEL PRESSURIZATION(10,1)\|WORKING SESSION(10,1)\|NA2O(9,4)\|CARBOXYMETHYLCELLULOSE(9,3)\|MAGNESIUM SILICATE WATER(8,5)\|SODIUM OLEATE(8,5)\|CEMENT PLANT(8,4)\|HOT GAS(8,4)\|R2SIO(8,4)\|ROTARY KILN(8,4)\|ACTINOLITE(8,2)\|AMOSITE(8,2)\|AMPHIBOLE(8,2)\|ANHYDROUS SODIUM CARBONATE(8,2)\|BRUCITE(8,2)\|CENTRIFUGATION(8,2)\|CHRYSOTILE(8,2)\|COMPLEX MAGNESIUM(8,2)\|CRYSTALLINE PHASE(8,2)\|ENSTATITE(8,2)\|FILTER CAKE MG(8,2)\|LIQUID FILTRATE(8,2)\|MEASURED LOI DATA(8,2)\|MG CONTENT(8,2)\|MGO SILICA MOLAR RATIO(8,2)\|MIXED POWDER(8,2)\|MR2MGSIO(8,2)\|PYROXENE(8,2)\|SIEVING(8,2)\|SODIUM CARBONATE POWDER(8,2)\|SYMBOL(8,2)\|TREMOLITE(8,2)\|ULTRASOUND(8,2)\|ALKALI BICARBONATE SOLUTION(8,1)\|ALKALI MAGNESIUM METAL ORTHOSILICATE(8,1)\|ALKALI SOLUBLE IMPURITY(8,1)\|BASIC MAGNESIUM ORTHOSILICATE(8,1)\|BIOMASS DERIVED FUEL(8,1)\|BLUE DIODE(8,1)\|CALCULATION MATRIX(8,1)\|CARBONATABLE SOLID(8,1)\|CARBONATE ION(8,1)\|CARBONATED PRODUCT(8,1)\|CHROMIUM CONTENT(8,1)\|CO2 GRAM(8,1)\|COARSE UNREACTED SOLID(8,1)\|COMBINED CO2 QUANTITATIVE DETECTION(8,1)\|COOLED PELLET(8,1)\|CRUSHED SAMPLE(8,1)\|HOT NODULE HEAT(8,1)\|HOT QUENCHED SOLID(8,1)\|INCOMING COMBUSTION AIR PREHEATER(8,1)\|MAGNESIA FINE PARTICLE(8,1)\|MAGNESIUM SILICATE MINERAL(8,1)\|MAJOR IMPURITY(8,1)\|MAXIMUM CO2 CAPTURE(8,1)\|MAXIMUM SLURRY ADDITIVE(8,1)\|NATURAL TALC(8,1)\|NATURALLY OCCURRING MINERAL(8,1)\|OUTGOING SOLID PARTICLE(8,1)\|PHASE PROBABILITY(8,1)\|PLUS MAGNESIUM(8,1)\|POROUS BED(8,1)\|POWDER SELF NODULIZE(8,1)\|PREHEATER TOP CYCLONE(8,1)\|QUALITATIVE PHASE(8,1)\|QUICK WASH(8,1)\|REACTION ESCAPE(8,1)\|REACTOR CONTENT(8,1)\|RED HE NE LASER(8,1)\|SESQUIHYDRATE(8,1)\|SILICA MOLE(8,1)\|SODIUM HYDROXIDE MILLIMOLE LITER(8,1)\|SOLUBLE SALT(8,1)\|SORT REACTION(8,1)\|STEEL CRUCIBLE(8,1)\|SULFUR CONTENT(8,1)\|TABLE EXPERIMENT(8,1)\|TREATED PELLET(8,1)\|TREATED SLURRY(8,1)\|WEAK PEAK(8,1)\|XRD DATA RIETVELD ANALYSIS(8,1)\|METHYL ISOBUTYL CARBINOL(7,5)\|NAFEO(7,2)\|SIEVE(7,2)\|DEIONIZED WATER(6,4)\|ATMOSPHERE PRESSURE(6,3)\|FE3O(6,3)\|H2SIO(6,3)\|HYDROXY CARBONATE WATER(6,3)\|USEFUL PRODUCT STREAM(6,3)\|XH2O(6,3)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|AIR BUBBLING(6,1)\|ALKALINE AQUEOUS SOLUTION(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANTHOPHYLLITE(6,1)\|ANTIGORITE(6,1)\|AQUEOUS ACID(6,1)\|AQUEOUS PHASE ICP ANALYSIS(6,1)\|ARLTHOPHYLLITE(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|CALCINATION(6,1)\|CAO SILICA MOLAR RATIO(6,1)\|CARBONATE PRODUCT(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|CRYSTALLINE PRODUCT(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|DURATIO N(6,1)\|EXCESS FERROUS SULFATE(6,1)\|FAYALITE(6,1)\|FE2SIO(6,1)\|	(EP2735553)\|1. A process for the treatment of a silicate mineral comprising:\| - a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate and a magnesium oxide, which step comprising the reaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula F2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4,\| - a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate,\|and\| - a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product\|2. A process according to claim 1 in which the magnesium silicate is a magnesium silicate in which the molar ratio of magnesium oxide to silica is from 1 to 3.\|3. A process according to any one of claims 1 to 2 in which the magnesium silicate comprises a magnesium silicate rock of the general composition:\| m(MgO)•t(QO)•SiO2•xH2O\|wherein m is from 1 to 3, t is less than or equal to 1, x is from zero to 2, and Q represents a metal or metals other than magnesium.\|4. A process according to any one of the preceding claims further comprising subsequent steps of (i) carbonation of the second product to produce a carbonated third product and (ii) partial dehydration of the carbonated third product to produce a fourth product.\|5. A process according to any one of claims 1 to 3 further comprising subsequent steps of (i) carbonation of the second product to produce a third product comprising magnesium hydroxide and an alkali metal carbonate and (ii) calcining the magnesium hydroxide in the third product to produce a fifth product comprising magnesium oxide.\|6. A process according to claim 3 in which Q represents iron, nickel and/or chromium which process further comprises isolation of an iron, nickel or chromium compound,	(EP2735553)\|[0001] This invention relates to a process for the treatment of a silicate mineral, The process uses as starting material a magnesium silicate and produces an alkali metal magnesium orthosilicate and magnesium oxide each of which can be isolated or subjected to further treatment to produce other products.\|[0002] US5085838 discloses preparation of a product comprising an alkali metal magnesium orthosilicate and a magnesium oxide, in which an alkali metal carbonate compound is reacted with a magnesium silicate.\|[0003] US2012291675 and US2004213705 describe processes for the sequestration of CO2 WO20070159902 discloses a method for industrial manufacture of pure MgCO3 from an olivine containing species of rock.\|[0004] XP2994928 describes a process where sodium bicarbonate, sodium chloride and water are mixed with magnesium silicates.\|[0005] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into common magnesium silicate hydrate minerals such as serpentine (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10(OH)2). Magnesium silicate rocks constitute an excellent source of two important elements, magnesium and silicon, in their oxide forms (MgO and SiO2). Processes to extract these two oxides from such rocks have heretofore been excessively energy-intensive and thus have not been commercialized.\|[0006] Although the magnesium silicate minerals tend to be very "unreactive," (e,g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a "carbonate fusion", is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analyzed by standard chemical techniques, thus allowing for total elemental analysis of the rock The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0007] The term sodium magnesium silicate is sometimes used, in accordance with the International Nomenclature of Cosmetic Ingredients (INCI) to identify synthetic hectorites in the form of nanoparticles and which form clear gels in water According to one manufacturer of such products hectorites have the formula (Mg5.2Li0.8)(Si8)O20(OH)4Na0.8.\|[0008] The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|[0009] The present invention accordingly provides a process for the treatment of a silicate mineral comprising a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate of the general formula R2MgSiO4 wherein R represents an alkali metal, and magnesium oxide which process comprises the reaction, at a temperature from 500 to 200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate, and a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product.\|[0010] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate, expressed as silicon dioxide, is preferably from <4:1 to 1:4, more preferably from 3:1 to 1:3, for example 2:1 to 1:2. The ratio is most preferably about 1.\|[0011] The alkali metal is preferably potassium or, more preferably, sodium.\|[0012] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used in the process of the invention.\|[0013] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0014] The magnesium silicate used in the process of the invention is generally a mineral silicate, for example a rock comprising a high concentration, preferably 20% or more, more preferably 50% or more, of a magnesium silicate of general composition:\| m(MgO)•t(QO)•SiO3•xH2O\|wherein m is from 1 to 3, t is less than or equal to 1, and x is from zero to 2: and Q represents a metal or metals other than magnesium, (for example calcium and/or a transition group metal such as iron, chromium or nickel). It will be understood that the composition or formulae of minerals is often depicted in terms of the theoretical amount of oxides which they contain: the oxides are, however, not present as such in the minerals whose composition is depicted in this way.\|[0015] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc, iddingsite and hectorite. These minerals may contain substantial quantities of iron in addition to magnesium and silicon, and also significant amounts of calcium, aluminium and alkali metals,\|[0016] Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, arlthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0017] The mineral silicate used in the process of the invention is preferably a magnesium silicate. The MgO/SiO2 molar ratio is 1-3. The CaO/SiO2 molar ratio is preferably ≤0.5. The FeO/SiO2 molar ratio is preferably ≤0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≤0.2.\|[0018] The alkali metal carbonate compound used in the process of the invention may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2•2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g chlorides, sulfates, sulphites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates or hydroxides) are present which, at the temperature used in the process of the invention, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0019] The process of the invention is preferably effected at a temperature from 600 to 1100°C, more preferably from 800 to 1000°C. Heating is generally effected for a few minutes to a few hours.\|[0020] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is solid or liquid.\|[0021] According to a feature of the invention the process is effected at a temperature below the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound.\|[0022] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as "R2O" in which R is as hereinbefore defined present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt. = 140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt. = 106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0023] The magnesium silicate and alkali metal carbonate compound used in the process of the present invention are preferably in particulate form or in shaped form, e.g. as pellets.\|[0024] Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the process of the invention will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of a fine sand (grain size 0.06 to 0.2mm) or, if necessary, ground to a fine powder (grain sizes below 0.06mm). Grain sizes greater than 0.06mm are generally determined by sieving. Grain sizes lower than 0.06mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0025] In one embodiment the process of the invention is conducted in a moving grate furnace. This procedure is especially suited to magnesium silicate rocks (rocks comprising mainly MgO and SiO2) in which the MgO/SiO2 molar ratio is close to or greater than 1.\|[0026] A mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in Figure 1 of the accompanying drawings.\|[0027] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0028] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone ("burning zone") just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1a) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate (R2CO3)\| (1a) Mg2SiO4 + R2CO3 ⇒ MgO + R2MgSiO4 + CO2↑\|in which R is as hereinbefore defined. The more general form of this reaction can be written as in equation (1 b) for m>=1 and equation 1 (c) for m<1:\| (1b) m(MgO)•t(QO)•SiO2•xH2O + R2CO3 ⇒ (m-1)MgO + R2MgSiO4 + tQO + CO2↑ + xH2O↑\| (1c) m(MgO)•t(QO)•SiO2•xH2O + R2CO3 ⇒ (1-m)R2SiO3 + mR2MgSiO4 + tQO + CO2↑ + xH2O↑\|wherein m is greater than or equal to 1 for reaction (1 b) and less than or equal to 1 for reaction (1 c); and Q, t and x are as hereinbefore defined. The vertical arrows T indicate that the carbon dioxide gas and water vapour produced by this reaction escape from the bed and exits with the rest of the exhaust gases. Thus, ideally, the final solid product remaining in the treated pellets is an intimate mixture comprising magnesium oxide (MgO also known as periclase) and alkali metal magnesium orthosilicate (R2MgSiO4) and/or alkali metal silicates (R2SiO3) as well as other solid products comprising the other metals (Q), especially iron, which may present as magnetite (Fe3O4) or possibly as an alkali metal ferrite (RFeO2), calcium, which may be present as silicates, chromium, which may be present as alkali metal chromates (R2CrO4), and nickel, which may be present as oxides.\|[0029] The idealized reactions depicted in equations (1 a,b,c) illustrate the production of alkali metal magnesium orthosilicates plus magnesium and/or other oxides and silicates by direct reaction of a stoichiometric (i.e. 1:1 R2O:SiO2) mixture of a magnesium silicate and an alkali metal carbonate.\|[0030] This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 3.4 kJ (i.e. about 0.8 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, there will be a significant net energy consumption for the overall process. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0031] In a further embodiment, the process of the invention is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln for the process of the invention which comprises a decarbonation step which produces carbon dioxide.\|[0032] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0033] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 35% of the total solids volume. However, since the reaction itself produces no liquid products (only solids and gases) at the temperatures preferably employed, the risk of the nodules deforming significantly due to melting is quite low even at far higher initial volume fractions of alkali metal carbonate as long as the heating occurs slowly enough to allow for a significant degree of reaction to occur before complete melting of the alkali metal carbonate.\|[0034] According to a further feature of the invention the process of the invention is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The nodules are then decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0035] The decarbonated and cooled pellets or nodules, comprising alkali metal magnesium orthosilicate and magnesium oxide or alkali metal silicate, are treated in order to separate the reaction products.\|[0036] In the process of the invention the first product comprising alkali metal magnesium orthosilicate and magnesium oxide is contacted with water to form a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate.\|[0037] The first product as, for example pellets or nodules, is preferably quenched in an amount of water, such that the final mixture after quenching has a temperature close to, but not exceeding, about 100°C, i.e. enough to quench the solids but avoiding excessive evaporation of water. The hot quenched solids are then preferably crushed and agitated mechanically in the form of a slurry. More water may be added if necessary. Some additional heating may be necessary.\|[0038] Alternatively the treatment with water, for example in the quenching and slurry-formation process described above, can be conducted at a temperature above 100°C if a pressurized vessel (e.g. an autoclave) is used.\|[0039] Alternatively the above quenching and slurry-formation process can be conducted at lower or ambient temperatures. Water for converting the first product into the second product can optionally be recycled from another part of the process.\|[0040] The objective is to separate the components of the second product by virtue of the facts that (a) alkali metal carbonates, silicates, chromates, sulfates and oxides or hydroxides in the product will tend to dissolve readily in water; (b) alkali metal magnesium orthosilicates will tend to hydrate in hot water to release alkali metals into solution as silicates and hydroxides, the remainder giving a fine suspension of solid magnesium silicate hydrates, and (c) magnesium oxide (MgO, also known as periclase) in the sample will tend to hydrate in hot water to give magnesium hydroxide (Mg(OH)2, also known as brucite) to form a soft and easily-dispersible powder.\|[0041] The slurry may need to be agitated mechanically. Then, the liquid phase can be separated from the bulk of the unreacted alkali metal magnesium orthosilicate and other unreacted anhydrous compounds, for example by sieving, and the fine particles of magnesium hydroxide and/or magnesium silicate hydrates which pass through the sieve as a slurry may be separated from the slurry by, for example, filtering, passage through a hydrocyclone, settling and/or centrifuging. The aqueous phase after separation of the magnesium hydroxide comprises an aqueous solution of alkali metal silicates and hydroxides.\|[0042] Alternatively, the separation process may be conducted in two steps, the first step comprising a rapid washing process to remove most of the readily soluble alkali metal carbonates, silicates and hydroxides; and the second step, conducted with additional water, comprising further hydration of both the magnesium oxide and the alkali metal magnesium orthosilicate. In this two-step approach, the water temperature is preferably lower for the first step (for example lower than 60°C) than for the second step, and an autoclave may be used for the second step if necessary.\|[0043] The overall result of the separation process described above can be summarized as follows: Solid products from the process of the invention, e.g. from the furnace or kiln, (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4, MgO or R2SiO3, QO, and possibly some residual R2CO3) are contacted with water to produce a second product comprising:\| (a) a fine suspension comprising Mg(OH)2 and/or magnesium silicate hydrates in a highly alkaline solution rich in alkali metal silicates, hydroxides and carbonates, and\| (b) coarse unreacted solids comprising R2MgSiO4, MgO, QO and unreacted particles of the original magnesium silicate rock (e.g. Mg2SiO4), and which separate easily by sedimentation (e.g. in a hydrocyclone) from the fine suspension.\|The fine suspension can then be further separated (e.g. by filtration) to give\| (c) fine solids rich in Mg(OH)2 and/or magnesium silicate hydrates, and\| (d) a solution rich in alkali metal silicates, hydroxides and carbonates, and also comprising minor amounts of alkali-soluble impurities, e.g. sulfates and chromates.\|[0044] The initial part of the reaction of the solid products in the process with water can be written qualitatively as follows, for m≥1 (equation 2a), and m≤1 (equation 2b):\| (2a) (m-1)MgO + R2MgSiO4 ⇒ (m-1)Mg(OH)2 + "M-S-H" + 2R+ + (OH-, H2SiO4=, CO3=)\| (2b) (1-m)R2SiO3 + mR2MgSiO4 ⇒ "M-S-H" + 2R+ + (OH-, H2SiO4=, CO3=)\|[0045] In the above reactions, the main solid compounds produced are an amorphous magnesium silicate hydrate, "M-S-H", of variable composition, plus, in the case where m>1, magnesium hydroxide (brucite). The alkali metals may dissolve completely in the aqueous phase as alkali metal cations (R+), and the charge of these alkali metal cations is balanced by a mixture of three principal dissolved anions: hydroxide (OH-), silicate (H2SiO4=) and carbonate (CO3=), present in various ratios depending on the conditions and materials used. It is to be understood that equations 2(a) and 2(b) are not perfectly balanced equations but rather are simply intended to indicate the main initial products of the reaction between the solid products of the process of the invention with water.\|[0046] In a further embodiment of the invention the alkaline solution produced in step (d) is contacted with a carbon dioxide-containing gas, for example combustion exhaust gases, to absorb carbon dioxide and yield an alkali metal carbonate, alkali metal bicarbonate or a mixture thereof, generally in solution, and (precipitated) silica.\|[0047] For example, the aqueous solution from step (d) comprising mainly alkali metal hydroxides and silicates and also some residual alkali metal carbonates is contacted with a carbon dioxide-containing gas, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. The solution rapidly absorbs CO2 from such gases to produce a solution of alkali metal carbonates and bicarbonates, and a precipitate of amorphous silica, according to the following, or similar, equations:\| (3) CO2 (gas) + 2ROH (in solution) ⇒ R2CO3 (in solution)\| (4) CO2(gas) + R2SiO3 (in solution) ⇒ R2CO3 (in solution) + SiO2 (solid precipitate)\| (5) CO2 (gas) + R2CO3 (in solution) ⇒ 2RHCO3 (in solution)\|[0048] The resulting solid silica precipitate is separated from the solution, for example by filtering, passage through a hydrocyclone, settling and/or centrifuging. In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled. Additional solutes, e.g. known salts, may also be incorporated into the solution. The precipitated silica formed by reaction (4) above can be separated, washed and dried for use in various applications.\|[0049] It will be understood by mass balance that reactions (3) and (4) should in principle be able to absorb essentially all of the CO2 released by the chemical reaction occurring in the process of the invention as shown in reaction (1), but that the additional CO2 resulting from the combustion process required to heat the starting materials will require an additional reaction to absorb it completely, e.g. either a reaction such as (5), or a further reaction with another absorbent.\|[0050] Magnesium hydroxide produced by the hydration of magnesium oxide prepared by the process of the invention also constitutes a feature of the invention. According to a further feature of the invention the magnesium hydroxide (preferably purified, for example by washing and drying) is calcined to produce magnesium oxide. It will be understood that the value of the magnesium hydroxide or magnesium oxide thus produced will depend mainly on the extent to which the major impurities (in this case, silica, iron compounds and alkali metal salts) are still present, which will be determined by the extent to which they are purified in additional steps such as washing and/or magnetic separation.\|[0051] In a further embodiment of the invention, the magnesium oxide, or magnesium hydroxide produced by the hydration of magnesium oxide, is contacted with a carbon dioxide-containing gas, preferably in the presence of water, to form a magnesium carbonate compound. The rate of this reaction can be controlled by the temperature, the pressure, the relative humidity, the presence of catalysts and/or the type of reactor used. The carbonation reaction is represented by the reaction:\| (6) CO2 (gas) + MgO or Mg(OH)2 ⇒ MgCO3 (solid, possibly hydrated)\|[0052] The products of this carbonation reaction may be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or complex magnesium hydroxy-carbonate hydrates, such as hydromagnesite (Mg(OH)2•4MgCO3•4H2O), or artinite (Mg(OH)2•MgCO3•3H2O), depending on the conditions employed.\|[0053] In a further embodiment of the invention the coarse, partially reacted solids separated from the reaction products in step 1(b) above comprise mainly unreacted magnesium silicate (for example, Mg2SiO4) mixed with some intermediate products (for example, Na2MgSiO4). These can be dried and recycled to be mixed with additional raw magnesium silicate starting material for feeding back into the process. It will be understood that drying should be accomplished in an energy-efficient manner, e.g. first by drainage and then by use of waste heat from the furnace or other sources.\|[0054] According to a further feature of the invention all of the solid products from the process of the invention, e.g. from the furnace or kiln (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4 and MgO and/or QO, and possibly some residual R2CO3 are ground together with water to produce a suspension or slurry which is then contacted with a gas containing carbon dioxide, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. During this treatment, in addition to the other reactions described above, (e.g. in equations (2), (3), (4), (5) and (6)), the alkali magnesium metal orthosilicate compound can also react directly with CO2 as indicated by equations (7) and (8) below:\| (7) R2MgSiO4 + 2CO2 ⇒ MgCO3 (solid) + SiO2 (solid) + R2CO3 (in solution)\|or, alternatively, making use of an alkali bicarbonate solution to achieve the same reaction:\| (8) R2MgSiO4 + 4RHCO3 ⇒ MgCO3 (solid) + SiO2 (solid) + 3R2CO3 (in solution)\|[0055] The alkali metal bicarbonate RHCO3 used in reaction (8) may be formed by the reaction of alkali metal carbonate solution R2CO3 produced in reaction (7) with carbon dioxide, as shown in equation (5).\|[0056] Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300°C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eiteleite, Na2CO3•MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|[0057] These types of reaction are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid products. The magnesium carbonate solid produced can be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or a complex magnesium hydroxy-carbonate hydrate, such as hydromagnesite (Mg(OH)2•4MgCO3•4H2O), or artinite (Mg(OH)2•MgCO3•3H2O), depending on the conditions and starting materials. The silica solid produced can be either a simple amorphous silica or a more complex mixed metal hydroxy-silicate such as a magnesium silicate hydrate ("M-S-H"). The alkali metal carbonate or bicarbonate solutions resulting from complete carbonation as shown in reactions (3), (4), (5), (7) and (8) can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and then recycled to the start of the process. The solid mixture of magnesium carbonates and silica produced by these reactions is one of the final products of the overall process and, after washing if necessary to recover as much as possible of the soluble alkali metal salts, can be separated for disposal or for use in other processes.\|[0058] The overall object of the process is to convert magnesium silicate rock into useful industrial products with low overall CO2 emissions. A further benefit of the process is to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable mineral carbonate which comprises a magnesium carbonate compound. Below are some examples of some different ways in which the process can be used:\| Starting with a magnesium silicate rock of composition m(MgO)•t(QO)•SiO2•xH2O, and recycling substantially all of the alkali metal (R) compounds used back into the process, at least two separate major product streams can be secured from amongst the following:(i) Products rich in magnesium oxide or hydroxide (MgO or Mg(OH)2)\| (ii) Products rich in amorphous silica (SiO2)\| (iii) Products rich in amorphous magnesium silicate hydrates (M-S-H)\| (iv) Products rich in magnesium carbonate compounds, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3 also known as magnesite); or magnesium carbonate trihydrate (MgCO3•3H2O, also known as nesquehonite); or magnesium hydroxy-carbonate hydrate, such as (Mg(OH)2•4MgCO3•4H2O), also known as hydromagnesite, or (Mg(OH)2•MgCO3•3H2O), also known as artinite.\|[0059] Improved separation of the above major solid product streams can also be achieved by the application of other known mineral separation techniques such as, for example, flotation. Such flotation techniques can be effected using flotation aids including sodium oleate, carboxymethylcellulose and methyl isobutyl carbinol.\|[0060] To the extent that CO2 is produced by the combustion of fuels used in the process, e.g. to heat the kiln or furnace, or to dry materials, this CO2 can be captured in the process in the form of product (iv) listed above, by using a treatment process based on the reactions shown above. To the extent that the process is energy-efficient, the aforesaid CO2 produced by the combustion of fuels used in the process, even if substantially completely captured by reactions of the sort shown, for example, in equations (3), (4) and (5), will generally not be sufficient to convert all of the magnesium in the process to product stream (iv), leaving some of the magnesium available for the production of product streams (i) and (iii). However, in another embodiment of the process, additional CO2 can be obtained from other sources and included in the treatment process and thus captured. In such a case, it is possible to operate the process in such a way that product stream (i) is not produced, but the process itself becomes a net consumer of CO2. Moreover, it is also possible to operate the process without separating any of the product streams, so that the only product stream produced is a mixture of some or all of the above product streams\|[0061] In a further approach, (not according to the invention), the process uses the same magnesium silicate raw material as shown above, but in this case, not all of the alkali metal-rich products of the process are recycled within the process. It is therefore possible to have one or more additional product streams as well as those already listed above. For example, one very useful product stream is an alkali metal silicate, (R2SiO3) either in the form of an alkaline aqueous solution also containing alkali metal hydroxides and/or carbonates, or as a solid product, (for example, obtained by evaporation and/or crystallization).\|[0062] According to a feature of the invention the first product is contacted with water to produce a second product comprising magnesium hydroxide which process further comprises (i) carbonation of the second product to produce a carbonated third product and (ii) partial dehydration of the carbonated third product to produce a fourth product.\|[0063] According to a further feature of the invention the first product is contacted with water to produce a second product comprising magnesium hydroxide which process further comprises (i) carbonation of the second product to produce a third product comprising magnesium hydroxide and an alkali metal carbonate and (ii) calcining the magnesium hydroxide from the third product to produce a fifth product comprising magnesium oxide.\|[0064] A hydraulic binder, for example as described in WO2009/156740 A1, comprises the fourth product. The hydraulic binder may further comprise an alkali metal carbonate from the third product. The hydraulic binder may further comprise magnesium oxide from the fifth product.\|[0065] The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|[0066] Another useful product stream is rich in transition metal oxides, for example iron oxides such as magnetite (Fe3O4 and which may also contain significant amounts of chromium and/or nickel oxides. These oxides can be concentrated by flotation and/or magnetic separation.\|[0067] Another useful product stream is an alkaline solution containing chromates, which can be treated with a reducing agent and pH control (or by electrochemical reduction) to separate relatively pure chromium oxides, or even chromium metal; for example:\| R2CrO4(aqueous solution) + (reducing agent) ⇒ Cr(OH)3 (solid precipitate)\|[0068] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0069] The term "pellets" as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0070] Particle size distribution when measured by laser granulometry is measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He-Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.\|[0071] The apparatus is checked before each working session by means of a standard sample (Sifraco C10 silica) for which the particle size distribution is known.\|[0072] Measurements are performed with the following parameters: pump speed 2300rpm and stirrer speed 800rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30s (for possible air bubbles to clear), a measurement is carried out for 15 s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0073] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0074] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R,Q, m, t, x and, p are as initially defined.\|[0075] The following non-limiting Examples illustrate embodiments of the invention.\|[0076] The following abbreviations and notations are used:\|XRF X-ray fluorescence\|XRD X-ray diffraction\|ICP Inductively-Coupled Plasma Photometry\|Hydromagnesite Mg(OH)2•4MgCO3•4H2O\|Artinite Mg(OH)2•MgCO3•3H2O\|Eitelite Na2CO3•Mg(CO3)\|LOI Loss on ignition\|EXAMPLE 1\|[0077] Ground pure olivine sand (Mg0.94Fe0.06)2SiO4 was mixed with sodium carbonate hydrate powder in a 14:11 mass ratio. The molar ratio of this mixture is close to 1:1. 25g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800°C over 2 hours, maintained at 800°C for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table.\|TABLE 1\|SampleLoss on IgnitionSodium carbonate powder14.97 %Ground olivine sand0.22 %14:11 mix of ground olivine sand + sodium carbonate powder16.69 %\|[0078] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by XRD. The reaction products observed by this technique were Na2MgSiO4, MgO and Fe2O3 together with some unreacted olivine and sodium carbonate.\|[0079] 10g of the reacted sample was put into 100 ml of de-ionised water under constant stirring at 40°C for 1h in order to evaluate its dissolution behaviour. The solution was filtered and the solid residue was analysed by XRD. The amounts of dissolved elements in the aqueous solutions were measured by ICP.\|[0080] The main solid phases detected in the filtered solid residue were Na2MgSiO4 MgO, Fe2O3 and olivine. All non-reacted sodium carbonate dissolved in the aqueous solution. Additionally, some dissolved SiO2 was detected with a concentration of 667 mg/l. From this value, one can estimate that 2 to 3% of the total silica from the mixture dissolved in the water under these conditions, (presumed to be as a sodium silicate, as the pH of the solution was measured to be about 12).\|EXAMPLE 2\|[0081] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. The molar ratio of this mixture is approximately 1:1. The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900°C. The sample was air-quenched after 1 h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851 °C). The measured loss on ignition of all of the samples is presented in the following Table.\|TABLE 2\|SampleLoss on IgnitionSodium carbonate14.96 %Olivine0.04 %Olivine + Sodium carbonate23.02 %\|[0082] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by XRD and the phases detected were Na2MgSiO4, MgO, NaFeO2 together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data. The MgO to Na2MgSiO4 mass ratio was estimated by Rietveld analysis of the XRD data to be 14:86, in reasonable agreement with mass balance calculations.\|EXAMPLE 3\|[0083] 13g of the powdered product of Example 2 was mixed with 260 ml of water to give a slurry with about 50g/L solids concentration. This slurry was put in a closed pressure reactor with a total volume of 2 litres, maintained at 25°C. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas and the pH of the aqueous solution were recorded as functions of time and are presented in Figure 2. The rate of pressure drop indicates that the slurry captures gaseous CO2 rapidly, and, concurrently, the pH of the solution falls rapidly from an initial value of over 12 to a final value of about 8.5, consistent with the formation of a mixed sodium carbonate/bicarbonate solution. After this reaction the solids in the slurry were filtered and analysed by XRD. NaFeO2 was no longer detectable and the MgO:Na2MgSiO4 ratio had increased to an estimated value of 18:82, indicating that some sodium silicate had leached out of the Na2MgSiO4 phase into the solution and had then been carbonated.\|EXAMPLE 4\|[0084] 5g of the powdered product of Example 2 was mixed with 200 ml of water to give a slurry of about 25g/L solids concentration. This slurry was then boiled gently for one hour, after which it was filtered and the solid residue analyzed by XRD. The relative concentration of the Na2MgSiO4 phase in the residue was clearly greatly reduced compared to the original untreated residue, and the relative concentration of MgO greatly increased. The NaFeO2 phase had also completely disappeared but peaks for a layered double hydroxide phase probably having a formula close to 4MgO•Fe2O3•CO2•10H2O were seen clearly, together with weaker peaks for Fe2O3 (haematite) and unreacted olivine.\|[0085] The liquid filtrate was also analyzed by ICP and the results (see the Table below) showed a high concentration (6.92 g/L as Na2O) of sodium in solution, as well as 0.47 g/L of SiO2. This confirms that most of the sodium had leached out of the sample, and that about 15% of it was probably in the form of a sodium metasilicate solution, the rest presumed to be a mixture of sodium hydroxide and sodium carbonate.\|Chemical analysis of the aqueous solution\|TABLE 3\|[0086] Chemical speciesConcentration [mg/l]SiO2466Al2O36.65Fe2O31.78CaO0.51MgO1.51K2O2.40Na2O6920SO32.53P0.58\|EXAMPLE 5\|[0087] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 litres, maintained at 35°C and agitated with a mechanical stirrer operating at 500rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its absorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in the following Table.\|TABLE 4\|Experiment n°Total CO2 captured (mol)Slurry volume (mL)Slurry conc. (g/L)Total solids. (g)CO2 captured, as % of theoretical maximumSlurry additivesTemp. (°C)Duration (h)Solid products detected10.06412605013.035Na2CO3: 21.15 g/L3524Hydromagne site20.07242605013.040Na2CO3: 53.85 g/L3524Hydromagne site30.13632605013.075NaHCO3: 53.85 g/L3530Hydromagne site40.035226011.52.99843526Artinite\|[0088] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite and, in one case, artinite, which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 6\|[0089] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometre sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950°C), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio (molar ratio approximately 1:1.3). About 5kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950°C for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by XRF spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3 and 33.4% sodium expressed as Na2O. An XRD analysis showed the major phases present in the product to be Na2MgSiO4 and periclase (MgO).\|EXAMPLE 7\|[0090] The reaction products of Example 2 (referred to hereinafter as "product X") and of Example 6 (referred to hereinafter as "product XS") were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75g of the solid were added to 1.5 litres of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal litres per hour at close to one atmosphere absolute pressure. The reactor contents were maintained at 70°C by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements by ICP. The solid filter-cakes were dried at 110°C and then analysed by XRF spectrometry for elemental composition, by XRD for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0091] The results for three different product samples are given in the following Table\|TABLE 5\|Experiment N° ; anhydrous product usedDuration (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %5 Product X3.5420Hydromagnesite31.215.918.20.65961 Product X4.0600Hydromagnesite30.316.418.80.5637 Product XS4.0205Hydromagnesite27.717.219.70.471(1) In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0092] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields of the order of 60-70% of the total magnesium in the starting material in about 3.5 to 4 hours. Based on XRF analyses of the solid phases coupled with ICP analyses of the liquid phase, it is estimated that roughly 90% of the initial Na and 50% of the initial Cr in the product leached out during the experiment.\|EXAMPLE 8\|Formation of eitelite.\|[0093] The procedure of Example 7 was repeated using two slurries (prepared from products X and XS from Examples 2 and 6, respectively) at a concentration of 150g/L, i.e. three times the concentration used in Example 7.\|[0094] During the 3 first hours the same trends were observed as those in Example 7. But after 4 hours, XRD revealed the presence of eitelite as well as hydromagnesite. The results are given in the following Table.\|TABLE 6\|Experiment N° ; anhydrous product usedDuratio n (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %8 Product X4.0600Hydromagnesite & eitelite28.0616.4518.830.567.129 Product XS4.0600Hydromagnesite & eitelite25.7415.8218.110.870.37\|EXAMPLE 9\|Effectiveness of water leaching\|[0095] 50g of product X was washed in 1 L deionised water 6 times in series (15minutes stirring in between at room temperature and atmospheric pressure, i.e. 25°C and 1 bar). Each time a small sample was taken to analyse the solids and the liquids. The XRF results for product X coupled with ICP solution analyses lead to the results given in the following Table, which the percentages of each element leached from the product are given as a function of the number of washing steps.\|TABLE 7\|% leachedSiCaMgKNaSCrWashing 19.850.460.0019.7636.4413.7746.12Washing 23.200.090.001.948.690.601.30Washing 31.410.020.000.253.470.040.21Washing 41.220.020.000.033.530.130.32Washing 50.750.020.000.021.870.140.12Washing 60.510.050.000.001.300.050.08TOTAL16.940.660.0122.0055.3114.7348.15\|[0096] The first washing step was clearly the most efficient. Therefore 500g of product X were washed in the same conditions, the solid was then filtered and dried overnight at 110°C. Finally the same carbonation experiment as described in Example 8 was performed on this solid product. This time XRD analysis revealed only hydromagnesite; no eitelite was detected. This shows that washing can be used to enhance Na recycling in the process.\|[0097] The analysis of the solution obtained after the first washing (table below) showed it to have a high pH and to contain about 4000mg/L of Na and 637 mg/L of Si, the other elements being present in much smaller amounts. On this basis, the solution was estimated to contain about 23 milimoles/litre of sodium metasilicate (Na2SiO3 and 130 millimoles/litre of sodium hydroxide (NaOH), possibly also including some carbonate ions.\|TABLE 8\|In mg/l (elements)SiCaMgKNaSCrWashing 1637.50.2990.2674.140001.38\|EXAMPLE 10\|Hydromagnesite formation at 60°C\|[0098] 1 L of a 50g/L slurry of product X was prepared and poured into a 2L autoclave. The system was closed and 1 L of pure CO2 at 10 bars was added without purging the residual air, after which the slurry was stirred and heated up to 60°C (which roughly corresponds to the dew point of exhaust gases in a cement plant). After 2 hours the pressure dropped to close to atmospheric and heating of the autoclave was stopped. The next day, the slurry was filtered and dried overnight at 110°C. XRD revealed hydromagnesite as the main crystalline product.\|EXAMPLE 11\|Formation of magnesite as main product at 120°C.\|[0099] The procedure of Example 10 was repeated but at 120°C (a typical temperature for exhaust gases from a cement plant) using the same autoclave, and adding CO2 each time the pressure dropped close to two bars (the equilibrium water vapour pressure at 120°C). Three additions of CO2 up to 10 bars were made in the space of one day. XRD on the dried solid revealed magnesite (MgCO3 to be the main product, but also showed some traces of magnetite (Fe3O4). ICP analysis of the aqueous phase showed 90% leaching of Na. The combined CO2 content in the solids was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser and showed that the amount of MgCO3 present accounted for about 47% of the original Mg in Product X.\|EXAMPLE 12\|Selective separation of chromium by reduction in solution.\|[0100] Powdered product X was stirred with deionised water for 15 minutes at a 2:1 water:solids mass ratio. The yellow-coloured aqueous phase was filtered and a sample taken for ICP analysis. Excess ferrous sulfate (FeSO4), a reducing agent, was then added in powder form to the solution, after which a chromium-containing precipitate formed. The liquid was again filtered, giving a colourless solution which was again analysed by ICP. The chromium content of the yellow-coloured aqueous phase was 772 mg/L. The colourless solution contained only 29 mg/L of chromium.\|[0101] These results, when compared with the analysis of the raw materials, indicated that about 50% of the total chromium in the original raw material (olivine) was converted into a readily soluble (chromate) form by the process used to make "product X," and 96% of the Cr leached into the solution was precipitated by addition of ferrous sulfate.\|EXAMPLE 13\|Concentration of hydromagnesite from the solid residues by flotation\|[0102] Separation tests were performed by flotation on the carbonated products produced from the application of the process to olivine and serpentine, similarl to the products shown, respectively, for experiments 5 and 7 in the table of Example 7. Combinations of sodium oleate, carboxymethylcellulose (CMC) and methyl isobutyl carbinol (MIBC) were used in the aqueous phase sequentially to disperse the solids in the form of a slurry at a solids concentration of 90g/L.\|[0103] First sodium oleate was added to the slurry and stirred for 5 minutes in a beaker in order to render carbonated particles hydrophobic. Then CMC was added to depress silicate hydrophobicity, followed by a further 5 minutes of stirring; and finally MIBC was added in order to stabilise the foam formed by air bubbling.\|[0104] Air was bubbled through the treated slurry in a miniature flotation cell, and the solids carried over by the foam were collected as "concentrate." The residual solids were collected as "tailings." Results of four such experiments are presented in the table below. The CO2 content was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser. The CO2 contents of the concentrates were typically 3-4 times greater than those of the tailings, showing that hydromagnesite can be effectively separated by flotation in this manner.\|[0105] The XRD results confirm the separation. They are expressed in a qualitative way by different symbols expressing the probability of a phase presence:\| (o) not present,\| () possibly present,\| (X) definitely present,\| (X+) present in abundance.\|TABLE 9\|Chemical additive (dosage, ppm)Test 1Test 2Test 3Test 4Sodium oleate1500100020001000CMC200200200200MIBC20202020Product tested by flotation:Carbonated "product X"Carbonate "product X"Carbonated "product X"Carbonated "product XS"Results of flotati on testsTailingsCon centrateTailingsConcentrateTailingsConcentrateTailingsConcentrateComponents measured by chemical analysisSiO2 %34.117.633.718.533.822.033.316.9Fe2O3 %6.43.46.43.66.44.36.93.0MgO %34.637.234.537.233.936.929.235.9Na2O %2.31.32.31.42.61.32.31.2LOI %22.340.022.638.922.735.126.241.6CO2 %5.722.25.820.25.717.39.423.0Phases detected by XRDSodium magnesium silicate00000000PericlaseXXX*OlivineXXX00HydromagnesiteXX+XX+XX+XX+\|EXAMPLE 14\|[0106] (not according to the invention) Ground natural talc from Luzenac (France) with nominal composition Mg3Si4O10(OH)2 and containing some minor impurities (1.1% Al2O3, 0.9 % Fe2O3 and 0.9% CaO by mass) was mixed with anhydrous sodium carbonate (Na2CO3) at a 4863:5136 mass ratio (molar ratio approximately 1:1). The composition was chosen in order to obtain an atomic ratio of 2:1 Na:Si in the final sample. 20.5g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. The sample was heated at 900°C for 1 hour, followed by cooling in air. It was weighed before and after treatment and the measured loss on ignition of 23.3% was consistent with evaporation of carbon dioxide from the sodium carbonate plus bound water from the talc; it represents about 95% of the theoretical value for complete reaction of 24.6%. The phase constitution of the reacted sample was determined by X-ray diffraction: the main products detected were Na2MgSiO4 and Na2SiO3.	(EP2735553)\|[0001] This invention relates to a process for the treatment of a silicate mineral, The process uses as starting material a magnesium silicate and produces an alkali metal magnesium orthosilicate and magnesium oxide each of which can be isolated or subjected to further treatment to produce other products.\|[0002] US5085838 discloses preparation of a product comprising an alkali metal magnesium orthosilicate and a magnesium oxide, in which an alkali metal carbonate compound is reacted with a magnesium silicate.\|[0003] US2012291675 and US2004213705 describe processes for the sequestration of CO2 WO20070159902 discloses a method for industrial manufacture of pure MgCO3 from an olivine containing species of rock.\|[0004] XP2994928 describes a process where sodium bicarbonate, sodium chloride and water are mixed with magnesium silicates.\|[0005] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into common magnesium silicate hydrate minerals such as serpentine (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10(OH)2). Magnesium silicate rocks constitute an excellent source of two important elements, magnesium and silicon, in their oxide forms (MgO and SiO2). Processes to extract these two oxides from such rocks have heretofore been excessively energy-intensive and thus have not been commercialized.\|[0006] Although the magnesium silicate minerals tend to be very "unreactive," (e,g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a "carbonate fusion", is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analyzed by standard chemical techniques, thus allowing for total elemental analysis of the rock The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0007] The term sodium magnesium silicate is sometimes used, in accordance with the International Nomenclature of Cosmetic Ingredients (INCI) to identify synthetic hectorites in the form of nanoparticles and which form clear gels in water According to one manufacturer of such products hectorites have the formula (Mg5.2Li0.8)(Si8)O20(OH)4Na0.8.\|[0008] The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|[0009] The present invention accordingly provides a process for the treatment of a silicate mineral comprising a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate of the general formula R2MgSiO4 wherein R represents an alkali metal, and magnesium oxide which process comprises the reaction, at a temperature from 500 to 200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate, and a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product.\|[0010] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate, expressed as silicon dioxide, is preferably from <4:1 to 1:4, more preferably from 3:1 to 1:3, for example 2:1 to 1:2. The ratio is most preferably about 1.\|[0011] The alkali metal is preferably potassium or, more preferably, sodium.\|[0012] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used in the process of the invention.\|[0013] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0014] The magnesium silicate used in the process of the invention is generally a mineral silicate, for example a rock comprising a high concentration, preferably 20% or more, more preferably 50% or more, of a magnesium silicate of general composition:\| m(MgO)•t(QO)•SiO3•xH2O\|wherein m is from 1 to 3, t is less than or equal to 1, and x is from zero to 2: and Q represents a metal or metals other than magnesium, (for example calcium and/or a transition group metal such as iron, chromium or nickel). It will be understood that the composition or formulae of minerals is often depicted in terms of the theoretical amount of oxides which they contain: the oxides are, however, not present as such in the minerals whose composition is depicted in this way.\|[0015] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc, iddingsite and hectorite. These minerals may contain substantial quantities of iron in addition to magnesium and silicon, and also significant amounts of calcium, aluminium and alkali metals,\|[0016] Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, arlthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0017] The mineral silicate used in the process of the invention is preferably a magnesium silicate. The MgO/SiO2 molar ratio is 1-3. The CaO/SiO2 molar ratio is preferably ≤0.5. The FeO/SiO2 molar ratio is preferably ≤0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≤0.2.\|[0018] The alkali metal carbonate compound used in the process of the invention may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2•2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g chlorides, sulfates, sulphites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates or hydroxides) are present which, at the temperature used in the process of the invention, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0019] The process of the invention is preferably effected at a temperature from 600 to 1100°C, more preferably from 800 to 1000°C. Heating is generally effected for a few minutes to a few hours.\|[0020] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is solid or liquid.\|[0021] According to a feature of the invention the process is effected at a temperature below the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound.\|[0022] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as "R2O" in which R is as hereinbefore defined present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt. = 140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt. = 106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0023] The magnesium silicate and alkali metal carbonate compound used in the process of the present invention are preferably in particulate form or in shaped form, e.g. as pellets.\|[0024] Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the process of the invention will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of a fine sand (grain size 0.06 to 0.2mm) or, if necessary, ground to a fine powder (grain sizes below 0.06mm). Grain sizes greater than 0.06mm are generally determined by sieving. Grain sizes lower than 0.06mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0025] In one embodiment the process of the invention is conducted in a moving grate furnace. This procedure is especially suited to magnesium silicate rocks (rocks comprising mainly MgO and SiO2) in which the MgO/SiO2 molar ratio is close to or greater than 1.\|[0026] A mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in Figure 1 of the accompanying drawings.\|[0027] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0028] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone ("burning zone") just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1a) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate (R2CO3)\| (1a) Mg2SiO4 + R2CO3 ⇒ MgO + R2MgSiO4 + CO2↑\|in which R is as hereinbefore defined. The more general form of this reaction can be written as in equation (1 b) for m>=1 and equation 1 (c) for m<1:\| (1b) m(MgO)•t(QO)•SiO2•xH2O + R2CO3 ⇒ (m-1)MgO + R2MgSiO4 + tQO + CO2↑ + xH2O↑\| (1c) m(MgO)•t(QO)•SiO2•xH2O + R2CO3 ⇒ (1-m)R2SiO3 + mR2MgSiO4 + tQO + CO2↑ + xH2O↑\|wherein m is greater than or equal to 1 for reaction (1 b) and less than or equal to 1 for reaction (1 c); and Q, t and x are as hereinbefore defined. The vertical arrows T indicate that the carbon dioxide gas and water vapour produced by this reaction escape from the bed and exits with the rest of the exhaust gases. Thus, ideally, the final solid product remaining in the treated pellets is an intimate mixture comprising magnesium oxide (MgO also known as periclase) and alkali metal magnesium orthosilicate (R2MgSiO4) and/or alkali metal silicates (R2SiO3) as well as other solid products comprising the other metals (Q), especially iron, which may present as magnetite (Fe3O4) or possibly as an alkali metal ferrite (RFeO2), calcium, which may be present as silicates, chromium, which may be present as alkali metal chromates (R2CrO4), and nickel, which may be present as oxides.\|[0029] The idealized reactions depicted in equations (1 a,b,c) illustrate the production of alkali metal magnesium orthosilicates plus magnesium and/or other oxides and silicates by direct reaction of a stoichiometric (i.e. 1:1 R2O:SiO2) mixture of a magnesium silicate and an alkali metal carbonate.\|[0030] This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 3.4 kJ (i.e. about 0.8 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, there will be a significant net energy consumption for the overall process. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0031] In a further embodiment, the process of the invention is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln for the process of the invention which comprises a decarbonation step which produces carbon dioxide.\|[0032] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0033] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 35% of the total solids volume. However, since the reaction itself produces no liquid products (only solids and gases) at the temperatures preferably employed, the risk of the nodules deforming significantly due to melting is quite low even at far higher initial volume fractions of alkali metal carbonate as long as the heating occurs slowly enough to allow for a significant degree of reaction to occur before complete melting of the alkali metal carbonate.\|[0034] According to a further feature of the invention the process of the invention is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The nodules are then decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0035] The decarbonated and cooled pellets or nodules, comprising alkali metal magnesium orthosilicate and magnesium oxide or alkali metal silicate, are treated in order to separate the reaction products.\|[0036] In the process of the invention the first product comprising alkali metal magnesium orthosilicate and magnesium oxide is contacted with water to form a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate.\|[0037] The first product as, for example pellets or nodules, is preferably quenched in an amount of water, such that the final mixture after quenching has a temperature close to, but not exceeding, about 100°C, i.e. enough to quench the solids but avoiding excessive evaporation of water. The hot quenched solids are then preferably crushed and agitated mechanically in the form of a slurry. More water may be added if necessary. Some additional heating may be necessary.\|[0038] Alternatively the treatment with water, for example in the quenching and slurry-formation process described above, can be conducted at a temperature above 100°C if a pressurized vessel (e.g. an autoclave) is used.\|[0039] Alternatively the above quenching and slurry-formation process can be conducted at lower or ambient temperatures. Water for converting the first product into the second product can optionally be recycled from another part of the process.\|[0040] The objective is to separate the components of the second product by virtue of the facts that (a) alkali metal carbonates, silicates, chromates, sulfates and oxides or hydroxides in the product will tend to dissolve readily in water; (b) alkali metal magnesium orthosilicates will tend to hydrate in hot water to release alkali metals into solution as silicates and hydroxides, the remainder giving a fine suspension of solid magnesium silicate hydrates, and (c) magnesium oxide (MgO, also known as periclase) in the sample will tend to hydrate in hot water to give magnesium hydroxide (Mg(OH)2, also known as brucite) to form a soft and easily-dispersible powder.\|[0041] The slurry may need to be agitated mechanically. Then, the liquid phase can be separated from the bulk of the unreacted alkali metal magnesium orthosilicate and other unreacted anhydrous compounds, for example by sieving, and the fine particles of magnesium hydroxide and/or magnesium silicate hydrates which pass through the sieve as a slurry may be separated from the slurry by, for example, filtering, passage through a hydrocyclone, settling and/or centrifuging. The aqueous phase after separation of the magnesium hydroxide comprises an aqueous solution of alkali metal silicates and hydroxides.\|[0042] Alternatively, the separation process may be conducted in two steps, the first step comprising a rapid washing process to remove most of the readily soluble alkali metal carbonates, silicates and hydroxides; and the second step, conducted with additional water, comprising further hydration of both the magnesium oxide and the alkali metal magnesium orthosilicate. In this two-step approach, the water temperature is preferably lower for the first step (for example lower than 60°C) than for the second step, and an autoclave may be used for the second step if necessary.\|[0043] The overall result of the separation process described above can be summarized as follows: Solid products from the process of the invention, e.g. from the furnace or kiln, (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4, MgO or R2SiO3, QO, and possibly some residual R2CO3) are contacted with water to produce a second product comprising:\| (a) a fine suspension comprising Mg(OH)2 and/or magnesium silicate hydrates in a highly alkaline solution rich in alkali metal silicates, hydroxides and carbonates, and\| (b) coarse unreacted solids comprising R2MgSiO4, MgO, QO and unreacted particles of the original magnesium silicate rock (e.g. Mg2SiO4), and which separate easily by sedimentation (e.g. in a hydrocyclone) from the fine suspension.\|The fine suspension can then be further separated (e.g. by filtration) to give\| (c) fine solids rich in Mg(OH)2 and/or magnesium silicate hydrates, and\| (d) a solution rich in alkali metal silicates, hydroxides and carbonates, and also comprising minor amounts of alkali-soluble impurities, e.g. sulfates and chromates.\|[0044] The initial part of the reaction of the solid products in the process with water can be written qualitatively as follows, for m≥1 (equation 2a), and m≤1 (equation 2b):\| (2a) (m-1)MgO + R2MgSiO4 ⇒ (m-1)Mg(OH)2 + "M-S-H" + 2R+ + (OH-, H2SiO4=, CO3=)\| (2b) (1-m)R2SiO3 + mR2MgSiO4 ⇒ "M-S-H" + 2R+ + (OH-, H2SiO4=, CO3=)\|[0045] In the above reactions, the main solid compounds produced are an amorphous magnesium silicate hydrate, "M-S-H", of variable composition, plus, in the case where m>1, magnesium hydroxide (brucite). The alkali metals may dissolve completely in the aqueous phase as alkali metal cations (R+), and the charge of these alkali metal cations is balanced by a mixture of three principal dissolved anions: hydroxide (OH-), silicate (H2SiO4=) and carbonate (CO3=), present in various ratios depending on the conditions and materials used. It is to be understood that equations 2(a) and 2(b) are not perfectly balanced equations but rather are simply intended to indicate the main initial products of the reaction between the solid products of the process of the invention with water.\|[0046] In a further embodiment of the invention the alkaline solution produced in step (d) is contacted with a carbon dioxide-containing gas, for example combustion exhaust gases, to absorb carbon dioxide and yield an alkali metal carbonate, alkali metal bicarbonate or a mixture thereof, generally in solution, and (precipitated) silica.\|[0047] For example, the aqueous solution from step (d) comprising mainly alkali metal hydroxides and silicates and also some residual alkali metal carbonates is contacted with a carbon dioxide-containing gas, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. The solution rapidly absorbs CO2 from such gases to produce a solution of alkali metal carbonates and bicarbonates, and a precipitate of amorphous silica, according to the following, or similar, equations:\| (3) CO2 (gas) + 2ROH (in solution) ⇒ R2CO3 (in solution)\| (4) CO2(gas) + R2SiO3 (in solution) ⇒ R2CO3 (in solution) + SiO2 (solid precipitate)\| (5) CO2 (gas) + R2CO3 (in solution) ⇒ 2RHCO3 (in solution)\|[0048] The resulting solid silica precipitate is separated from the solution, for example by filtering, passage through a hydrocyclone, settling and/or centrifuging. In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled. Additional solutes, e.g. known salts, may also be incorporated into the solution. The precipitated silica formed by reaction (4) above can be separated, washed and dried for use in various applications.\|[0049] It will be understood by mass balance that reactions (3) and (4) should in principle be able to absorb essentially all of the CO2 released by the chemical reaction occurring in the process of the invention as shown in reaction (1), but that the additional CO2 resulting from the combustion process required to heat the starting materials will require an additional reaction to absorb it completely, e.g. either a reaction such as (5), or a further reaction with another absorbent.\|[0050] Magnesium hydroxide produced by the hydration of magnesium oxide prepared by the process of the invention also constitutes a feature of the invention. According to a further feature of the invention the magnesium hydroxide (preferably purified, for example by washing and drying) is calcined to produce magnesium oxide. It will be understood that the value of the magnesium hydroxide or magnesium oxide thus produced will depend mainly on the extent to which the major impurities (in this case, silica, iron compounds and alkali metal salts) are still present, which will be determined by the extent to which they are purified in additional steps such as washing and/or magnetic separation.\|[0051] In a further embodiment of the invention, the magnesium oxide, or magnesium hydroxide produced by the hydration of magnesium oxide, is contacted with a carbon dioxide-containing gas, preferably in the presence of water, to form a magnesium carbonate compound. The rate of this reaction can be controlled by the temperature, the pressure, the relative humidity, the presence of catalysts and/or the type of reactor used. The carbonation reaction is represented by the reaction:\| (6) CO2 (gas) + MgO or Mg(OH)2 ⇒ MgCO3 (solid, possibly hydrated)\|[0052] The products of this carbonation reaction may be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or complex magnesium hydroxy-carbonate hydrates, such as hydromagnesite (Mg(OH)2•4MgCO3•4H2O), or artinite (Mg(OH)2•MgCO3•3H2O), depending on the conditions employed.\|[0053] In a further embodiment of the invention the coarse, partially reacted solids separated from the reaction products in step 1(b) above comprise mainly unreacted magnesium silicate (for example, Mg2SiO4) mixed with some intermediate products (for example, Na2MgSiO4). These can be dried and recycled to be mixed with additional raw magnesium silicate starting material for feeding back into the process. It will be understood that drying should be accomplished in an energy-efficient manner, e.g. first by drainage and then by use of waste heat from the furnace or other sources.\|[0054] According to a further feature of the invention all of the solid products from the process of the invention, e.g. from the furnace or kiln (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4 and MgO and/or QO, and possibly some residual R2CO3 are ground together with water to produce a suspension or slurry which is then contacted with a gas containing carbon dioxide, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. During this treatment, in addition to the other reactions described above, (e.g. in equations (2), (3), (4), (5) and (6)), the alkali magnesium metal orthosilicate compound can also react directly with CO2 as indicated by equations (7) and (8) below:\| (7) R2MgSiO4 + 2CO2 ⇒ MgCO3 (solid) + SiO2 (solid) + R2CO3 (in solution)\|or, alternatively, making use of an alkali bicarbonate solution to achieve the same reaction:\| (8) R2MgSiO4 + 4RHCO3 ⇒ MgCO3 (solid) + SiO2 (solid) + 3R2CO3 (in solution)\|[0055] The alkali metal bicarbonate RHCO3 used in reaction (8) may be formed by the reaction of alkali metal carbonate solution R2CO3 produced in reaction (7) with carbon dioxide, as shown in equation (5).\|[0056] Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300°C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eiteleite, Na2CO3•MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|[0057] These types of reaction are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid products. The magnesium carbonate solid produced can be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or a complex magnesium hydroxy-carbonate hydrate, such as hydromagnesite (Mg(OH)2•4MgCO3•4H2O), or artinite (Mg(OH)2•MgCO3•3H2O), depending on the conditions and starting materials. The silica solid produced can be either a simple amorphous silica or a more complex mixed metal hydroxy-silicate such as a magnesium silicate hydrate ("M-S-H"). The alkali metal carbonate or bicarbonate solutions resulting from complete carbonation as shown in reactions (3), (4), (5), (7) and (8) can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and then recycled to the start of the process. The solid mixture of magnesium carbonates and silica produced by these reactions is one of the final products of the overall process and, after washing if necessary to recover as much as possible of the soluble alkali metal salts, can be separated for disposal or for use in other processes.\|[0058] The overall object of the process is to convert magnesium silicate rock into useful industrial products with low overall CO2 emissions. A further benefit of the process is to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable mineral carbonate which comprises a magnesium carbonate compound. Below are some examples of some different ways in which the process can be used:\| Starting with a magnesium silicate rock of composition m(MgO)•t(QO)•SiO2•xH2O, and recycling substantially all of the alkali metal (R) compounds used back into the process, at least two separate major product streams can be secured from amongst the following:(i) Products rich in magnesium oxide or hydroxide (MgO or Mg(OH)2)\| (ii) Products rich in amorphous silica (SiO2)\| (iii) Products rich in amorphous magnesium silicate hydrates (M-S-H)\| (iv) Products rich in magnesium carbonate compounds, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3 also known as magnesite); or magnesium carbonate trihydrate (MgCO3•3H2O, also known as nesquehonite); or magnesium hydroxy-carbonate hydrate, such as (Mg(OH)2•4MgCO3•4H2O), also known as hydromagnesite, or (Mg(OH)2•MgCO3•3H2O), also known as artinite.\|[0059] Improved separation of the above major solid product streams can also be achieved by the application of other known mineral separation techniques such as, for example, flotation. Such flotation techniques can be effected using flotation aids including sodium oleate, carboxymethylcellulose and methyl isobutyl carbinol.\|[0060] To the extent that CO2 is produced by the combustion of fuels used in the process, e.g. to heat the kiln or furnace, or to dry materials, this CO2 can be captured in the process in the form of product (iv) listed above, by using a treatment process based on the reactions shown above. To the extent that the process is energy-efficient, the aforesaid CO2 produced by the combustion of fuels used in the process, even if substantially completely captured by reactions of the sort shown, for example, in equations (3), (4) and (5), will generally not be sufficient to convert all of the magnesium in the process to product stream (iv), leaving some of the magnesium available for the production of product streams (i) and (iii). However, in another embodiment of the process, additional CO2 can be obtained from other sources and included in the treatment process and thus captured. In such a case, it is possible to operate the process in such a way that product stream (i) is not produced, but the process itself becomes a net consumer of CO2. Moreover, it is also possible to operate the process without separating any of the product streams, so that the only product stream produced is a mixture of some or all of the above product streams\|[0061] In a further approach, (not according to the invention), the process uses the same magnesium silicate raw material as shown above, but in this case, not all of the alkali metal-rich products of the process are recycled within the process. It is therefore possible to have one or more additional product streams as well as those already listed above. For example, one very useful product stream is an alkali metal silicate, (R2SiO3) either in the form of an alkaline aqueous solution also containing alkali metal hydroxides and/or carbonates, or as a solid product, (for example, obtained by evaporation and/or crystallization).\|[0062] According to a feature of the invention the first product is contacted with water to produce a second product comprising magnesium hydroxide which process further comprises (i) carbonation of the second product to produce a carbonated third product and (ii) partial dehydration of the carbonated third product to produce a fourth product.\|[0063] According to a further feature of the invention the first product is contacted with water to produce a second product comprising magnesium hydroxide which process further comprises (i) carbonation of the second product to produce a third product comprising magnesium hydroxide and an alkali metal carbonate and (ii) calcining the magnesium hydroxide from the third product to produce a fifth product comprising magnesium oxide.\|[0064] A hydraulic binder, for example as described in WO2009/156740 A1, comprises the fourth product. The hydraulic binder may further comprise an alkali metal carbonate from the third product. The hydraulic binder may further comprise magnesium oxide from the fifth product.\|[0065] The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|[0066] Another useful product stream is rich in transition metal oxides, for example iron oxides such as magnetite (Fe3O4 and which may also contain significant amounts of chromium and/or nickel oxides. These oxides can be concentrated by flotation and/or magnetic separation.\|[0067] Another useful product stream is an alkaline solution containing chromates, which can be treated with a reducing agent and pH control (or by electrochemical reduction) to separate relatively pure chromium oxides, or even chromium metal; for example:\| R2CrO4(aqueous solution) + (reducing agent) ⇒ Cr(OH)3 (solid precipitate)\|[0068] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0069] The term "pellets" as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0070] Particle size distribution when measured by laser granulometry is measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He-Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.\|[0071] The apparatus is checked before each working session by means of a standard sample (Sifraco C10 silica) for which the particle size distribution is known.\|[0072] Measurements are performed with the following parameters: pump speed 2300rpm and stirrer speed 800rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30s (for possible air bubbles to clear), a measurement is carried out for 15 s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0073] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0074] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R,Q, m, t, x and, p are as initially defined.\|[0075] The following non-limiting Examples illustrate embodiments of the invention.\|[0076] The following abbreviations and notations are used:\|XRF X-ray fluorescence\|XRD X-ray diffraction\|ICP Inductively-Coupled Plasma Photometry\|Hydromagnesite Mg(OH)2•4MgCO3•4H2O\|Artinite Mg(OH)2•MgCO3•3H2O\|Eitelite Na2CO3•Mg(CO3)\|LOI Loss on ignition\|EXAMPLE 1\|[0077] Ground pure olivine sand (Mg0.94Fe0.06)2SiO4 was mixed with sodium carbonate hydrate powder in a 14:11 mass ratio. The molar ratio of this mixture is close to 1:1. 25g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800°C over 2 hours, maintained at 800°C for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table.\|TABLE 1\|SampleLoss on IgnitionSodium carbonate powder14.97 %Ground olivine sand0.22 %14:11 mix of ground olivine sand + sodium carbonate powder16.69 %\|[0078] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by XRD. The reaction products observed by this technique were Na2MgSiO4, MgO and Fe2O3 together with some unreacted olivine and sodium carbonate.\|[0079] 10g of the reacted sample was put into 100 ml of de-ionised water under constant stirring at 40°C for 1h in order to evaluate its dissolution behaviour. The solution was filtered and the solid residue was analysed by XRD. The amounts of dissolved elements in the aqueous solutions were measured by ICP.\|[0080] The main solid phases detected in the filtered solid residue were Na2MgSiO4 MgO, Fe2O3 and olivine. All non-reacted sodium carbonate dissolved in the aqueous solution. Additionally, some dissolved SiO2 was detected with a concentration of 667 mg/l. From this value, one can estimate that 2 to 3% of the total silica from the mixture dissolved in the water under these conditions, (presumed to be as a sodium silicate, as the pH of the solution was measured to be about 12).\|EXAMPLE 2\|[0081] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. The molar ratio of this mixture is approximately 1:1. The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900°C. The sample was air-quenched after 1 h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851 °C). The measured loss on ignition of all of the samples is presented in the following Table.\|TABLE 2\|SampleLoss on IgnitionSodium carbonate14.96 %Olivine0.04 %Olivine + Sodium carbonate23.02 %\|[0082] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by XRD and the phases detected were Na2MgSiO4, MgO, NaFeO2 together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data. The MgO to Na2MgSiO4 mass ratio was estimated by Rietveld analysis of the XRD data to be 14:86, in reasonable agreement with mass balance calculations.\|EXAMPLE 3\|[0083] 13g of the powdered product of Example 2 was mixed with 260 ml of water to give a slurry with about 50g/L solids concentration. This slurry was put in a closed pressure reactor with a total volume of 2 litres, maintained at 25°C. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas and the pH of the aqueous solution were recorded as functions of time and are presented in Figure 2. The rate of pressure drop indicates that the slurry captures gaseous CO2 rapidly, and, concurrently, the pH of the solution falls rapidly from an initial value of over 12 to a final value of about 8.5, consistent with the formation of a mixed sodium carbonate/bicarbonate solution. After this reaction the solids in the slurry were filtered and analysed by XRD. NaFeO2 was no longer detectable and the MgO:Na2MgSiO4 ratio had increased to an estimated value of 18:82, indicating that some sodium silicate had leached out of the Na2MgSiO4 phase into the solution and had then been carbonated.\|EXAMPLE 4\|[0084] 5g of the powdered product of Example 2 was mixed with 200 ml of water to give a slurry of about 25g/L solids concentration. This slurry was then boiled gently for one hour, after which it was filtered and the solid residue analyzed by XRD. The relative concentration of the Na2MgSiO4 phase in the residue was clearly greatly reduced compared to the original untreated residue, and the relative concentration of MgO greatly increased. The NaFeO2 phase had also completely disappeared but peaks for a layered double hydroxide phase probably having a formula close to 4MgO•Fe2O3•CO2•10H2O were seen clearly, together with weaker peaks for Fe2O3 (haematite) and unreacted olivine.\|[0085] The liquid filtrate was also analyzed by ICP and the results (see the Table below) showed a high concentration (6.92 g/L as Na2O) of sodium in solution, as well as 0.47 g/L of SiO2. This confirms that most of the sodium had leached out of the sample, and that about 15% of it was probably in the form of a sodium metasilicate solution, the rest presumed to be a mixture of sodium hydroxide and sodium carbonate.\|Chemical analysis of the aqueous solution\|TABLE 3\|[0086] Chemical speciesConcentration [mg/l]SiO2466Al2O36.65Fe2O31.78CaO0.51MgO1.51K2O2.40Na2O6920SO32.53P0.58\|EXAMPLE 5\|[0087] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 litres, maintained at 35°C and agitated with a mechanical stirrer operating at 500rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its absorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in the following Table.\|TABLE 4\|Experiment n°Total CO2 captured (mol)Slurry volume (mL)Slurry conc. (g/L)Total solids. (g)CO2 captured, as % of theoretical maximumSlurry additivesTemp. (°C)Duration (h)Solid products detected10.06412605013.035Na2CO3: 21.15 g/L3524Hydromagne site20.07242605013.040Na2CO3: 53.85 g/L3524Hydromagne site30.13632605013.075NaHCO3: 53.85 g/L3530Hydromagne site40.035226011.52.99843526Artinite\|[0088] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite and, in one case, artinite, which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 6\|[0089] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometre sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950°C), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio (molar ratio approximately 1:1.3). About 5kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950°C for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by XRF spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3 and 33.4% sodium expressed as Na2O. An XRD analysis showed the major phases present in the product to be Na2MgSiO4 and periclase (MgO).\|EXAMPLE 7\|[0090] The reaction products of Example 2 (referred to hereinafter as "product X") and of Example 6 (referred to hereinafter as "product XS") were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75g of the solid were added to 1.5 litres of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal litres per hour at close to one atmosphere absolute pressure. The reactor contents were maintained at 70°C by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements by ICP. The solid filter-cakes were dried at 110°C and then analysed by XRF spectrometry for elemental composition, by XRD for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0091] The results for three different product samples are given in the following Table\|TABLE 5\|Experiment N° ; anhydrous product usedDuration (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %5 Product X3.5420Hydromagnesite31.215.918.20.65961 Product X4.0600Hydromagnesite30.316.418.80.5637 Product XS4.0205Hydromagnesite27.717.219.70.471(1) In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0092] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields of the order of 60-70% of the total magnesium in the starting material in about 3.5 to 4 hours. Based on XRF analyses of the solid phases coupled with ICP analyses of the liquid phase, it is estimated that roughly 90% of the initial Na and 50% of the initial Cr in the product leached out during the experiment.\|EXAMPLE 8\|Formation of eitelite.\|[0093] The procedure of Example 7 was repeated using two slurries (prepared from products X and XS from Examples 2 and 6, respectively) at a concentration of 150g/L, i.e. three times the concentration used in Example 7.\|[0094] During the 3 first hours the same trends were observed as those in Example 7. But after 4 hours, XRD revealed the presence of eitelite as well as hydromagnesite. The results are given in the following Table.\|TABLE 6\|Experiment N° ; anhydrous product usedDuratio n (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %8 Product X4.0600Hydromagnesite & eitelite28.0616.4518.830.567.129 Product XS4.0600Hydromagnesite & eitelite25.7415.8218.110.870.37\|EXAMPLE 9\|Effectiveness of water leaching\|[0095] 50g of product X was washed in 1 L deionised water 6 times in series (15minutes stirring in between at room temperature and atmospheric pressure, i.e. 25°C and 1 bar). Each time a small sample was taken to analyse the solids and the liquids. The XRF results for product X coupled with ICP solution analyses lead to the results given in the following Table, which the percentages of each element leached from the product are given as a function of the number of washing steps.\|TABLE 7\|% leachedSiCaMgKNaSCrWashing 19.850.460.0019.7636.4413.7746.12Washing 23.200.090.001.948.690.601.30Washing 31.410.020.000.253.470.040.21Washing 41.220.020.000.033.530.130.32Washing 50.750.020.000.021.870.140.12Washing 60.510.050.000.001.300.050.08TOTAL16.940.660.0122.0055.3114.7348.15\|[0096] The first washing step was clearly the most efficient. Therefore 500g of product X were washed in the same conditions, the solid was then filtered and dried overnight at 110°C. Finally the same carbonation experiment as described in Example 8 was performed on this solid product. This time XRD analysis revealed only hydromagnesite; no eitelite was detected. This shows that washing can be used to enhance Na recycling in the process.\|[0097] The analysis of the solution obtained after the first washing (table below) showed it to have a high pH and to contain about 4000mg/L of Na and 637 mg/L of Si, the other elements being present in much smaller amounts. On this basis, the solution was estimated to contain about 23 milimoles/litre of sodium metasilicate (Na2SiO3 and 130 millimoles/litre of sodium hydroxide (NaOH), possibly also including some carbonate ions.\|TABLE 8\|In mg/l (elements)SiCaMgKNaSCrWashing 1637.50.2990.2674.140001.38\|EXAMPLE 10\|Hydromagnesite formation at 60°C\|[0098] 1 L of a 50g/L slurry of product X was prepared and poured into a 2L autoclave. The system was closed and 1 L of pure CO2 at 10 bars was added without purging the residual air, after which the slurry was stirred and heated up to 60°C (which roughly corresponds to the dew point of exhaust gases in a cement plant). After 2 hours the pressure dropped to close to atmospheric and heating of the autoclave was stopped. The next day, the slurry was filtered and dried overnight at 110°C. XRD revealed hydromagnesite as the main crystalline product.\|EXAMPLE 11\|Formation of magnesite as main product at 120°C.\|[0099] The procedure of Example 10 was repeated but at 120°C (a typical temperature for exhaust gases from a cement plant) using the same autoclave, and adding CO2 each time the pressure dropped close to two bars (the equilibrium water vapour pressure at 120°C). Three additions of CO2 up to 10 bars were made in the space of one day. XRD on the dried solid revealed magnesite (MgCO3 to be the main product, but also showed some traces of magnetite (Fe3O4). ICP analysis of the aqueous phase showed 90% leaching of Na. The combined CO2 content in the solids was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser and showed that the amount of MgCO3 present accounted for about 47% of the original Mg in Product X.\|EXAMPLE 12\|Selective separation of chromium by reduction in solution.\|[0100] Powdered product X was stirred with deionised water for 15 minutes at a 2:1 water:solids mass ratio. The yellow-coloured aqueous phase was filtered and a sample taken for ICP analysis. Excess ferrous sulfate (FeSO4), a reducing agent, was then added in powder form to the solution, after which a chromium-containing precipitate formed. The liquid was again filtered, giving a colourless solution which was again analysed by ICP. The chromium content of the yellow-coloured aqueous phase was 772 mg/L. The colourless solution contained only 29 mg/L of chromium.\|[0101] These results, when compared with the analysis of the raw materials, indicated that about 50% of the total chromium in the original raw material (olivine) was converted into a readily soluble (chromate) form by the process used to make "product X," and 96% of the Cr leached into the solution was precipitated by addition of ferrous sulfate.\|EXAMPLE 13\|Concentration of hydromagnesite from the solid residues by flotation\|[0102] Separation tests were performed by flotation on the carbonated products produced from the application of the process to olivine and serpentine, similarl to the products shown, respectively, for experiments 5 and 7 in the table of Example 7. Combinations of sodium oleate, carboxymethylcellulose (CMC) and methyl isobutyl carbinol (MIBC) were used in the aqueous phase sequentially to disperse the solids in the form of a slurry at a solids concentration of 90g/L.\|[0103] First sodium oleate was added to the slurry and stirred for 5 minutes in a beaker in order to render carbonated particles hydrophobic. Then CMC was added to depress silicate hydrophobicity, followed by a further 5 minutes of stirring; and finally MIBC was added in order to stabilise the foam formed by air bubbling.\|[0104] Air was bubbled through the treated slurry in a miniature flotation cell, and the solids carried over by the foam were collected as "concentrate." The residual solids were collected as "tailings." Results of four such experiments are presented in the table below. The CO2 content was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser. The CO2 contents of the concentrates were typically 3-4 times greater than those of the tailings, showing that hydromagnesite can be effectively separated by flotation in this manner.\|[0105] The XRD results confirm the separation. They are expressed in a qualitative way by different symbols expressing the probability of a phase presence:\| (o) not present,\| () possibly present,\| (X) definitely present,\| (X+) present in abundance.\|TABLE 9\|Chemical additive (dosage, ppm)Test 1Test 2Test 3Test 4Sodium oleate1500100020001000CMC200200200200MIBC20202020Product tested by flotation:Carbonated "product X"Carbonate "product X"Carbonated "product X"Carbonated "product XS"Results of flotati on testsTailingsCon centrateTailingsConcentrateTailingsConcentrateTailingsConcentrateComponents measured by chemical analysisSiO2 %34.117.633.718.533.822.033.316.9Fe2O3 %6.43.46.43.66.44.36.93.0MgO %34.637.234.537.233.936.929.235.9Na2O %2.31.32.31.42.61.32.31.2LOI %22.340.022.638.922.735.126.241.6CO2 %5.722.25.820.25.717.39.423.0Phases detected by XRDSodium magnesium silicate00000000PericlaseXXX*OlivineXXX00HydromagnesiteXX+XX+XX+XX+\|EXAMPLE 14\|[0106] (not according to the invention) Ground natural talc from Luzenac (France) with nominal composition Mg3Si4O10(OH)2 and containing some minor impurities (1.1% Al2O3, 0.9 % Fe2O3 and 0.9% CaO by mass) was mixed with anhydrous sodium carbonate (Na2CO3) at a 4863:5136 mass ratio (molar ratio approximately 1:1). The composition was chosen in order to obtain an atomic ratio of 2:1 Na:Si in the final sample. 20.5g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. The sample was heated at 900°C for 1 hour, followed by cooling in air. It was weighed before and after treatment and the measured loss on ignition of 23.3% was consistent with evaporation of carbon dioxide from the sodium carbonate plus bound water from the talc; it represents about 95% of the theoretical value for complete reaction of 24.6%. The phase constitution of the reacted sample was determined by X-ray diffraction: the main products detected were Na2MgSiO4 and Na2SiO3.	Family Number\|(66070146)\|66070146\|Advantages / Prev. Drawbacks\|(EP2735553 B1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|(EP2735553 A1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|	Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-2251/402\|B01D-2253/106\|B01D-2257/504\|C01B-033/20\|C01F-005/06\|C01F-005/14\|C01F-005/24\|C04B-002/10/2\|C04B-009/00\|C04B-028/10\|C04B-028/18/4\|C04B-2111/00019\|Y02C-020/40\|Y02P-020/151\|Y02P-040/18\|Y02P-040/40	(GR1) C04B-028/18/4[RK1]; C04B-040/02/31[RK2]	B01D-053/62\|B01D-2251/402\|B01D-2253/106\|B01D-2257/504\|C01B-033/20\|C01F-005/06\|C01F-005/14\|C01F-005/24\|C04B-002/10/2\|C04B-009/00\|C04B-028/10\|C04B-028/18/4\|C04B-2111/00019\|Y02C-020/40\|Y02P-020/151\|Y02P-040/18\|Y02P-040/40	B01D-053/62\|C01B-033/20\|C01D-007/00\|C01F-005/06\|C01F-005/14\|C01F-005/24\|C04B-002/10	B01D-053/62\|C01B-033/20\|C01D-007/00\|C01F-005/06\|C01F-005/14\|C01F-005/24\|C04B-002/10\|C04B-009/00			CN119370855	CN119370855 113183772 WHO=Examiner SELF=N CAT=A	US20120291675\|WO200769902\|US6054106\|WO2009156740\|EP2508496\|US5085838\|EP2532624\|WO201097451\|CA1189288\|US20120291675\|WO2009156740\|US20040213705\|US20040213705\|US5085838	US20120291675 6949869 WHO=Examiner SELF=N CAT=Y\|WO200769902 6679764 WHO=Examiner SELF=N CAT=Y\|US6054106 490034 WHO=Examiner SELF=N CAT=X CAT=Y\|WO2009156740 1844239 WHO=Examiner SELF=N CAT=X CAT=D\|EP2508496 15070805 WHO=Examiner SELF=N CAT=X\|US5085838 42717873 WHO=Examiner SELF=N CAT=X\|EP2532624 15065813 WHO=Examiner SELF=N CAT=E\|WO201097451 44611783 WHO=Examiner SELF=N CAT=A\|CA1189288 3817049 WHO=Examiner SELF=N CAT=A\|US20120291675 6949869 WHO=Applicant SELF=N\|WO2009156740 1844239 WHO=Applicant SELF=N\|US20040213705 1759232 WHO=Examiner SELF=N\|US20040213705 1759232 WHO=Applicant SELF=N\|US5085838 42717873 WHO=Applicant SELF=N		EP2532624; US5085838; EP2508496; US20120291675; WO200769902; CA1189288; WO201097451; US6054106; US20040213705; XP002994928; WO2009156740; US5085838; US20120291675; US20040213705; WO20070159902; WO2009156740	(EP2735553)\|Examiner references\|-O'CONNOR W K ET AL: "Carbon dioxide sequestration by direct mineral carbonation: process mineralogy of feed and products", MINERALS AND METALLURGICAL PROCESSING,, vol. 19, no. 2, 1 May 2002 (2002-05-01), pages 95 - 101, XP002994928, ISSN: 0747-9182\|	LAPSED	(EP2735553)\|LAPSED	DEAD	(EP2735553)\|DEAD	(EP2735553)\|LEGAL DETAILS FOR EP2735553\|Actual or expected expiration date=2020-10-30\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-11-27\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP12306468\|Application date=2012-11-27\|Standardized application number=2012EP-0306468\|Event publication date=2014-05-27\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2014-05-28\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication 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event=2019-11-27\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2020-10-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=GB\|MEMBER STATE LEGAL DETAILS FOR GR\|Actual or expected expiration date=2017-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GR\|Event publication date=2017-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=GR\|MEMBER STATE LEGAL 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notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=IE\|MEMBER STATE LEGAL DETAILS FOR IS\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IS\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IS\|MEMBER STATE LEGAL DETAILS FOR IT\|Actual or expected expiration date=2018-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2018-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IT\|MEMBER STATE LEGAL DETAILS FOR LI\|Actual or expected expiration date=2020-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LI\|Event publication date=2020-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LI\|MEMBER STATE LEGAL DETAILS FOR LT\|Actual or expected expiration date=2017-08-25\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2017-08-25\|Event code=EP/REG\|Event code=LT/MG4D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Invalidated european patent\|Europos patentai, laikomi ab initio negaliojanciais\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2017-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LT\|MEMBER STATE LEGAL DETAILS FOR LU\|Actual or expected expiration date=2018-08-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LU\|Event publication date=2018-08-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LU\|MEMBER STATE LEGAL DETAILS FOR LV\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LV\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LV\|MEMBER STATE LEGAL DETAILS FOR MC\|Actual or expected expiration date=2018-06-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MC\|Event publication date=2018-06-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MC\|MEMBER STATE LEGAL DETAILS FOR MK\|Actual or expected expiration date=2019-11-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MK\|Event publication date=2019-11-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MK\|MEMBER STATE LEGAL DETAILS FOR MT\|Actual or expected expiration date=2018-09-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MT\|Event publication date=2018-09-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=MT\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=2017-04-05\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2017-08-09\|Event code=EP/REG\|Event code=NL/MP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent voided (invalid in the netherlands as no translation has been filed)\|Effective date of the event=2017-04-05\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2017-09-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NL\|MEMBER STATE LEGAL DETAILS FOR NO\|Actual or expected expiration date=2017-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NO\|Event publication date=2017-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NO\|MEMBER STATE LEGAL DETAILS FOR PL\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PL\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PL\|MEMBER STATE LEGAL DETAILS FOR PT\|Actual or expected expiration date=2020-05-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PT\|Event publication date=2020-05-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PT\|MEMBER STATE LEGAL DETAILS FOR RO\|Actual or expected expiration date=2018-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RO\|Event publication date=2018-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RO\|MEMBER STATE LEGAL DETAILS FOR RS\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RS\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RS\|MEMBER STATE LEGAL DETAILS FOR SE\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SE\|MEMBER STATE LEGAL DETAILS FOR SI\|Actual or expected expiration date=2018-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SI\|Event publication date=2018-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SI\|MEMBER STATE LEGAL DETAILS FOR SK\|Actual or expected expiration date=2018-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SK\|Event publication date=2018-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SK\|MEMBER STATE LEGAL DETAILS FOR SM\|Actual or expected expiration date=2018-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SM\|Event publication date=2018-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SM\|MEMBER STATE LEGAL DETAILS FOR TR\|Actual or expected expiration date=2020-03-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=TR\|Event publication date=2020-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=TR	(EP2735553)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR		https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=9ru+nrv5jojEpfCxziNKemkyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP2735553&ekey=947&xpn=EP2735553&kind=B1	https://register.epo.org/application?number=EP12306468	https://permalink.orbit.com/RenderStaticFirstPage?XPN=ckl9VSHqF2eeccOAsqvWAnfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	EP	(EP2735553)\|FR\|(EP2735553)\|FR	(EP2735553)\|NAME=LAFARGE 61, rue des Belles Feuilles , CITY=75116 Paris , COUNTRY=FR , REG=100163084\|(EP2735553)\|NAME=LAFARGE 61, rue des Belles Feuilles , CITY=75116 Paris , COUNTRY=FR , REG=100163084	(EP2735553)\|AT\|(EP2735553)\|FR	(EP2735553)\|NAME=Keschmann, Marc;Haffner und Keschmann Patentanwälte GmbH Schottengasse 3a , CITY=1014 Wien , COUNTRY=AT , REG=101393339\|(EP2735553)\|NAME=Mérigeault, Shona;Lafarge Département Propriété Industrielle (DPI) 95 Rue du Montmurier BP 9 , CITY=38291 Saint Quentin Fallavier Cedex , COUNTRY=FR , REG=101004378	(EP2735553)\|FR; FR; FR\|(EP2735553)\|FR; FR; FR	(EP2735553)\|NAME=Gartner, Ellis Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=Pisch, Alexander Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=Meyer, Vincent Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR\|(EP2735553)\|NAME=Gartner, Ellis Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=Pisch, Alexander Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=Meyer, Vincent Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR	(EP2735553)\|2	1	1					(EP2735553)\|Number of Claims: NCL=6\|Primary examiner: Theodoridou, K\|\|(EP2735553)\|Number of Claims: NCL=10\|Primary examiner: Theodoridou, K\|		(EP2735553)\|ENGLISH (ENG)	(EP2735553)\|Patent\|(EP2735553)\|Patent	Titre: (EP2735553)\|Process for the treatment of a silicate mineral Résumé: (EP2735553)\|The invention provides a process for the preparation of a first product comprising an alkali metal magnesium orthosilicate and (i) magnesium oxide or (ii) an alkali metal silicate, which process comprises the reaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R 2 O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO 2 , being from 4:1 to 1:4, and contacting the first product with water to produce a second product comprising magnesium hydroxide and isolating or producing further useful products from the second product.	42	Abstract	gpt-4o-mini	uncertain	The process involves silicate minerals and alkali metal carbonates, but it is not explicitly focused on CO₂ capture or enhanced weathering for carbon sequestration.
46	EP12306468\|EP12306469\|EP13795508\|WOEP2013/074732	WOEP2013/074732\|RU2015125492\|AU2013351282\|CN201380061823\|US14/647,277\|JP2015543468\|EP13795508\|MX2015006607\|KR10-2015-7016739\|CA2892325	RU2654983\|AU2013351282\|CN104812468\|US9631257\|RU2015125492\|JP2015536897\|US20150299823\|EP2925426\|MX2015006607\|KR10-2015-0088845\|CN104812468\|AU2013351282\|CA2892325\|WO2014/082996	66131709	WO2014/082996 A1 2014-06-05 [WO201482996]\|RU2654983 C2 2018-05-23 [RU2654983]\|RU2015125492 A 2017-01-11 [RU2015125492]\|AU2013351282 B2 2018-03-01 [AU2013351282]\|AU2013351282 A1 2015-06-18 [AU2013351282]\|CN104812468 B 2017-08-25 [CN104812468B]\|CN104812468 A 2015-07-29 [CN104812468]\|US9631257 B2 2017-04-25 [US9631257]\|US20150299823 A1 2015-10-22 [US20150299823]\|JP2015536897 A 2015-12-24 [JP2015536897]\|EP2925426 A1 2015-10-07 [EP2925426]\|MX2015006607 A 2015-08-05 [MX2015006607]\|KR10-2015-0088845 A 2015-08-03 [KR20150088845]\|CA2892325 A1 2014-06-05 [CA2892325]	2012-11-27\|2013-11-26	2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26	2018-05-23\|2018-03-01\|2017-08-25\|2017-04-25\|2017-01-11\|2015-12-24\|2015-10-22\|2015-10-07\|2015-08-05\|2015-08-03\|2015-07-29\|2015-06-18\|2014-06-05\|2014-06-05	\|(US9631257)\|2017-04-25\|\|\|(CN104812468B)\|2017-08-25\|(RU2654983)\|2018-05-23\|(AU2013351282)\|2018-03-01\|\|\|	(EP2925426)\|2018-04-10\|(US9631257)\|2021-05-31\|(WO2014/082996)\|2016-05-27\|(JP2015536897)\|2018-08-22\|(CN104812468)\|2019-11-26\|(RU2654983)\|2019-11-27\|(AU2013351282)\|2020-06-25\|(MX2015006607)\|2033-11-26\|(KR10-2015-0088845)\|2018-12-27\|(CA2892325)\|2020-08-31	(EP2925426)\|Process for the treatment of a silicate mineral	(EP2925426)\|The invention provides a process for the preparation of a second composition, said process comprising the steps of: -preparing a first compositioncomprising an alkali metal magnesium orthosilicate andoptionally either(i) magnesium oxide or(ii) an alkali metal silicate, byreaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R 2 O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO 2, being from 4:1 to 1:4, and -contacting the first composition with water to produce thesecond composition comprising an amorphous magnesium silicate hydrate (M-S-H). It is possible to isolateor producefurther useful products from the second composition.	HOLCIM TECHNOLOGY\|LAFARGE	(EP2925426)\|Lafarge SA ([FR])\|(US9631257)\|LAFARGE ([FR])\|(US20150299823)\|LAFARGE ([FR])\|(WO2014/082996)\|LAFARGE ([FR])\|(JP2015536897)\|LAFARGE SA\|(CN104812468)\|LAFARGE SA ([FR])\|(CN104812468)\|LAFARGE SA ([FR])\|(RU2654983)\|LAFARGE ([FR])\|(RU2015125492)\|LAFARGE ([FR])\|(AU2013351282)\|Lafarge\|(AU2013351282)\|Lafarge\|(MX2015006607)\|LAFARGE ([FR])\|(KR10-2015-0088845)\|LAFARGE\|(CA2892325)\|LAFARGE ([FR])	PISCH ALEXANDER\|GARTNER ELLIS\|MEYER VINCENT	(EP2925426)\|PISCH, Alexander\|GARTNER, Ellis\|MEYER, Vincent	(EP2925426)\|Soares, Luis Filipe;Lafarge ([FR])\|Reg. Nb: 101513670\|(US9631257)\|Pillsbury Winthrop Shaw Pittman LLP\|(WO2014/082996)\|MERIGEAULT, Shona ([FR])\|(JP2015536897)\|MURAKOSHI, Satoshi\|Reg. Nb: 100126572\|OBATA Yuichi\|Reg. Nb: 100125195\|(CN104812468)\|CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11314\|(RU2654983)\|LLC LAW FIRM GORODISSKY AND PARTNERS\|(AU2013351282)\|Watermark Intellectual Property Pty Ltd ([AU])\|(MX2015006607)\|CARLOS PÉREZ DE LA SIERRA\|(KR10-2015-0088845)\|KOREANA PATENT FIRM\|Reg. Nb: 920011000013\|(CA2892325)\|NORTON ROSE FULBRIGHT CANADA LLP/S.E.N.C.R.L., S.R.L. ([CA])	(US9631257)\|However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible.\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled.\|Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300° C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eitelite, Na2CO3.MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|	(US9631257)\|1. A process for the treatment of a silicate mineral, said process comprising: preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 600° C. to 1000° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, wherein the reaction is obtained by contacting the alkali metal carbonate compound and the magnesium silicate to each other in a solid state, and contacting the first composition with water to produce a second composition comprising an amorphous magnesium silicate hydrate (M-S-H).\|	(US9631257)\|It was found to contain nesquehonite (MgCO3.3H2O), nahcolite (NaHCO3), trona (Na3H(CO3)2.2H2O), and sodium carbonate mono-hydrate (Na2CO3.H2O).\|The present invention accordingly provides a process for the preparation of a second composition, said process comprising the steps of: - preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 500 to 1200° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, and - contacting the first composition with water to produce the second composition comprising an amorphous magnesium silicate hydrate (M-S-H).\|This invention relates to a process for the treatment of a silicate mineral.\|	(EP2925426)\|SILICATE MINERAL(100,1)\|SILICATE MINERAL TREATMENT(100,1)\|\|(US9631257)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,4)\|SILICATE MINERAL TREATMENT(100,4)\|MAGNESIUM SILICATE(94,63)\|AMORPHOUS SILICA PRECIPITATE(80,2)\|SILICA PRECIPITATE(70,1)\|ALKALI METAL CARBONATE(68,49)\|MAGNESIUM ORTHOSILICATE(66,14)\|OUTGOING HOT GAS(64,1)\|MOLAR RATIO(62,11)\|MOVING GRATE FURNACE(62,2)\|OUTGOING HOT SOLID(58,1)\|NA2CO(57,2)\|ALKALI METAL SILICATE(56,12)\|ALKALI METAL(54,76)\|MAGNESIUM SILICATE HYDRATE(54,6)\|SUBSTEP(54,2)\|ALKALI METAL BICARBONATE(52,5)\|NEUTRALIZING(50,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(48,12)\|INCOMING SOLID(48,1)\|NAHCOLITE(48,1)\|MAGNESIUM OXIDE(44,16)\|FURNACE(42,8)\|MOVING GRATE(38,5)\|INCOMING COMBUSTION AIR(38,1)\|NET ENERGY CONSUMPTION(37,2)\|USEFUL PRODUCT(37,2)\|METHANEDIONE(36,5)\|COUNTERCURRENT HEAT EXCHANGE(36,3)\|TEMPERATURE ELEVATION(36,1)\|CARBONATED SHAPED ARTICLE(35,3)\|NESQUEHONITE(34,7)\|PELLET(33,24)\|MGCO(33,14)\|EITELITE(31,5)\|CO2(29,29)\|AMBIENT TEMPERATURE(28,2)\|MAGNESIUM OXIDE MOLAR RATIO(28,1)\|X H2O(26,1)\|UNREACTED OLIVINE(24,3)\|COMPLEX ALKALI METAL(24,1)\|SODIUM CARBONATE MONO HYDRATE(24,1)\|BED(23,5)\|HEAT EXCHANGE(22,4)\|PREHEATER CYCLONE TOWER(22,1)\|OLIVINE SAND(21,3)\|PLATINUM CRUCIBLE(21,3)\|SOLID PRODUCT(20,10)\|LAB FURNACE(20,4)\|XRF SPECTROMETRY(20,2)\|R2MGSIO(18,9)\|GASEOUS CO2(18,4)\|SODIUM BICARBONATE(18,2)\|ASBESTOS FIBRILLAR(18,1)\|DECARBONATED NODULE(18,1)\|MAGNESIUM XRD SILICATE(18,1)\|OBSCURATION STABILIZATION(18,1)\|EARTH CRUST(17,2)\|LASER GRANULOMETRY(17,2)\|RESIDUAL R2CO(17,2)\|MG2SIO(16,7)\|FINE SUSPENSION(16,4)\|CHROMIUM COMPOUND(16,3)\|COUNTER CURRENT HEAT EXCHANGE(16,1)\|DECARBONATED PELLET(16,1)\|FORSTERITE OLIVINE(16,1)\|METHANEDIONE GAS LIBERATION(16,1)\|NA2MGSIO(14,6)\|TAILING(14,6)\|ENERGY EFFICIENCY(14,3)\|SAMPLE REACTION(14,3)\|ANHYDROUS MAGNESIUM SILICATE(14,2)\|SLURRY ADDITIVE(14,2)\|ABSORB METHANEDIONE(14,1)\|CO2 NET CONSUMER(14,1)\|CO2 SLURRY(14,1)\|DISSOLUTION BEHAVIOR(14,1)\|HEAT TRANSFER(14,1)\|HELICOIDAL TEFLON(14,1)\|MAGNETITE TRACE(14,1)\|METHANEDIONE EVAPORATION(14,1)\|MINIATURE FLOTATION CELL(14,1)\|PHOTOMETRY HYDROMAGNESITE MG(14,1)\|PREHEATER TOWER(14,1)\|SILICATE HYDROPHOBICITY(14,1)\|MAGNESIUM SILICATE WATER(13,11)\|ALKALI METAL OXIDE(13,7)\|AUTOCLAVE(13,5)\|PERICLASE(13,5)\|HUMIDITY CONDITION(13,4)\|PARTICULATE(12,4)\|POWDERED PRODUCT(12,4)\|PRODUCT RICH(12,4)\|BURNING ZONE(12,2)\|BLAINE MG(12,1)\|CARBONATE PARTICLE(12,1)\|CO2 UPTAKE(12,1)\|COMPANION PELLET(12,1)\|CONCENTRATE CO2 CONTENT(12,1)\|EFFLORESCENCE SAMPLE(12,1)\|ENHANCE NA RECYCLING(12,1)\|GROUND OLIVINE MIX(12,1)\|LASER GRANULOMETER(12,1)\|NODULE RISK(12,1)\|PERFECTLY BALANCED EQUATION(12,1)\|PRODUCT HECTORITE MANUFACTURER(12,1)\|SAMPLE DEAGGLOMERATION(12,1)\|SLURRY TEMP(12,1)\|SUSPENSION PREHEATER(12,1)\|UNREACTED ANHYDROUS COMPOUND(12,1)\|UNTREATED PELLET(12,1)\|UNTREATED RESIDUE(12,1)\|ANHYDROUS DURATION PRODUCT(11,2)\|COLORLESS SOLUTION(11,2)\|GAS ANALYZER(11,2)\|MGO EXPRESSION(11,2)\|REACTED SAMPLE PHASE CONSTITUTION(11,2)\|SI CA MG(11,2)\|SODIUM MAGNESIUM ORTHOSILICATE(11,2)\|REACTION PRODUCT(10,8)\|ALKALINE SOLUTION(10,3)\|COMBUSTION EXHAUST GAS(10,3)\|HYDROCYCLONE(10,3)\|QUENCHING(10,3)\|ANALYSIS NA2O(10,1)\|ARTINITE MG(10,1)\|CO2 10H2O(10,1)\|CO2 EMISSION(10,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(10,1)\|CURING REGIME(10,1)\|DECARBONATION REACTION(10,1)\|EARTH MANTLE COMPONENT(10,1)\|EXPERIMENT CAPTURED VOLUME(10,1)\|FERMENTATION RESIDUE GAS(10,1)\|FINE NESS(10,1)\|FINE SAND GRANULOMETRY(10,1)\|FLOTATION AID(10,1)\|INORGANIC IMPURITY(10,1)\|LAYERED DOUBLE HYDROXIDE(10,1)\|MINERAL CARBONATE(10,1)\|MOVING GRATE COOLER(10,1)\|OLIVINE SAMPLE(10,1)\|PRECIPITATED SILICA(10,1)\|R2O MOLAR RATIO(10,1)\|RAW MAGNESIUM SILICATE(10,1)\|SILICATE ANION(10,1)\|SUSPENSION AGITATION(10,1)\|SYNTHETIC HECTORITE(10,1)\|UNREACTED MAGNESIUM SILICATE(10,1)\|UNREACTED PARTICLE(10,1)\|VESSEL PRESSURIZATION(10,1)\|WET CARBONATED PELLET(10,1)\|WORKING SESSION(10,1)\|R2SIO(9,5)\|SODIUM OLEATE(9,5)\|CARBOXYMETHYLCELLULOSE(9,3)\|CEMENT PLANT(8,4)\|HOT GAS(8,4)\|HYDROXY CARBONATE WATER(8,4)\|ROTARY KILN(8,4)\|ACTINOLITE(8,2)\|AMOSITE(8,2)\|AMPHIBOLE(8,2)\|ANHYDROUS SODIUM CARBONATE(8,2)\|ANTHOPHYLLITE(8,2)\|BRUCITE(8,2)\|CENTRIFUGATION(8,2)\|CHRYSOTILE(8,2)\|COMPLEX MAGNESIUM(8,2)\|ENSTATITE(8,2)\|LIQUID FILTRATE(8,2)\|MEASURED LOI DATA(8,2)\|MGO SILICA MOLAR RATIO(8,2)\|MIXED POWDER(8,2)\|MOLDING(8,2)\|PYROXENE(8,2)\|SIEVING(8,2)\|SODIUM CARBONATE POWDER(8,2)\|SYMBOL(8,2)\|TREMOLITE(8,2)\|ULTRASOUND(8,2)\|ALKALI BICARBONATE SOLUTION(8,1)\|ALKALI SOLUBLE IMPURITY(8,1)\|BASIC MAGNESIUM ORTHOSILICATE(8,1)\|BIOMASS DERIVED FUEL(8,1)\|BLUE DIODE(8,1)\|CALCULATION MATRIX(8,1)\|CARBONATABLE SOLID(8,1)\|CARBONATE ION(8,1)\|CARBONATED PRODUCT(8,1)\|CHROMIUM CONTENT(8,1)\|CO2 ATMOSPHERE(8,1)\|CO2 GRAM(8,1)\|COARSE UNREACTED SOLID(8,1)\|COMBINED CO2 QUANTITATIVE DETECTION(8,1)\|COMPRESSIVE LOAD(8,1)\|COOLED PELLET(8,1)\|CRUSHED SAMPLE(8,1)\|CRYSTALLINE COMPOUND(8,1)\|CURING CHAMBER(8,1)\|CYLINDRICAL MOLD(8,1)\|CYLINDRICAL PELLET(8,1)\|DISSOLVED ANION(8,1)\|ESTIMATED MG(8,1)\|GROUND NATURAL TALC(8,1)\|HOT NODULE HEAT(8,1)\|HOT QUENCHED SOLID(8,1)\|INCOMING COMBUSTION AIR PREHEATER(8,1)\|IRON ISOLATION(8,1)\|MAGNESIA FINE PARTICLE(8,1)\|MAGNESIUM SILICATE MINERAL(8,1)\|MAXIMUM CO2 CAPTURE(8,1)\|NATURALLY OCCURRING MINERAL(8,1)\|OUTGOING SOLID PARTICLE(8,1)\|PHASE PROBABILITY(8,1)\|PLUS MAGNESIUM(8,1)\|POROUS BED(8,1)\|POWDER SELF NODULIZE(8,1)\|PREHEATER TOP CYCLONE(8,1)\|PRESSED PELLET(8,1)\|QUALITATIVE PHASE(8,1)\|QUICK WASH(8,1)\|REACTION ESCAPE(8,1)\|REACTOR CONTENT(8,1)\|RED HE NE LASER(8,1)\|RUBBER BOWL(8,1)\|SESQUIHYDRATE(8,1)\|SILICA MOLE(8,1)\|SODIUM SILICATE MILIMOLE LITER(8,1)\|SOLUBLE SALT(8,1)\|SORT REACTION(8,1)\|STEEL CRUCIBLE(8,1)\|SULFUR CONTENT(8,1)\|TREATED SLURRY(8,1)\|WEAK PEAK(8,1)\|XRD DATA RIETVELD ANALYSIS(8,1)\|DEIONIZED WATER(7,5)\|METHYL ISOBUTYL CARBINOL(7,5)\|ALKALI METAL CATION(7,3)\|ATMOSPHERE PRESSURE(7,3)\|DRY CONDITION(7,3)\|FE3O(7,3)\|USEFUL PRODUCT STREAM(7,3)\|NAFEO(7,2)\|SIEVE(7,2)\|4MGO FE2O(6,1)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|AIR BUBBLING(6,1)\|ALKALINE AQUEOUS SOLUTION(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANHYDROUS PRODUCT(6,1)\|ANTIGORITE(6,1)\|AQUEOUS ACID(6,1)\|AQUEOUS PHASE ICP ANALYSIS(6,1)\|AQUEOUS SOLUTION CHEMICAL SPECIES(6,1)\|ATMOSPHERIC PRESSURE CARBONATION(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|CALCINATION(6,1)\|CAO SILICA MOLAR RATIO(6,1)\|CARBONATE PRODUCT(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|CO2 MG(6,1)\|COMPRESSION MACHINE(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|CRYSTALLINE PRODUCT(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|EXCESS FERROUS SULFATE(6,1)\|FAYALITE(6,1)\|FE2SIO(6,1)\|FEO SILICA MOLAR RATIO(6,1)\|FILTER CAKE DRYING(6,1)\|\|(US20150299823)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,4)\|SILICATE MINERAL TREATMENT(100,4)\|MAGNESIUM SILICATE(89,62)\|AMORPHOUS SILICA PRECIPITATE(80,2)\|SILICA PRECIPITATE(70,1)\|MAGNESIUM ORTHOSILICATE(66,14)\|OUTGOING HOT GAS(64,1)\|ALKALI METAL CARBONATE(63,48)\|MOLAR RATIO(62,11)\|MOVING GRATE FURNACE(62,2)\|OUTGOING HOT SOLID(58,1)\|NA2CO(57,2)\|ALKALI METAL SILICATE(56,12)\|MAGNESIUM SILICATE HYDRATE(54,6)\|SUBSTEP(54,2)\|ALKALI METAL(52,75)\|ALKALI METAL BICARBONATE(52,5)\|CARBONATED SHAPED ARTICLE(52,4)\|NEUTRALIZING(50,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(48,12)\|INCOMING SOLID(48,1)\|NAHCOLITE(48,1)\|MAGNESIUM OXIDE(44,16)\|FURNACE(42,8)\|MOVING GRATE(38,5)\|INCOMING COMBUSTION AIR(38,1)\|NET ENERGY CONSUMPTION(37,2)\|USEFUL PRODUCT(37,2)\|METHANEDIONE(36,5)\|COUNTERCURRENT HEAT EXCHANGE(36,3)\|TEMPERATURE ELEVATION(36,1)\|NESQUEHONITE(34,7)\|PELLET(33,24)\|MGCO(33,14)\|EITELITE(31,5)\|CO2(29,29)\|AMBIENT TEMPERATURE(28,2)\|MAGNESIUM OXIDE MOLAR RATIO(28,1)\|MOLDING(24,3)\|UNREACTED OLIVINE(24,3)\|COMPLEX ALKALI METAL(24,1)\|SODIUM CARBONATE MONO HYDRATE(24,1)\|BED(23,5)\|HEAT EXCHANGE(22,4)\|PREHEATER CYCLONE TOWER(22,1)\|OLIVINE SAND(21,3)\|PLATINUM CRUCIBLE(21,3)\|SOLID PRODUCT(20,10)\|LAB FURNACE(20,4)\|XRF SPECTROMETRY(20,2)\|GASEOUS CO2(18,4)\|SODIUM BICARBONATE(18,2)\|ASBESTOS FIBRILLAR(18,1)\|DECARBONATED NODULE(18,1)\|MAGNESIUM XRD SILICATE(18,1)\|OBSCURATION STABILIZATION(18,1)\|EARTH CRUST(17,2)\|LASER GRANULOMETRY(17,2)\|RESIDUAL R2CO(17,2)\|R2MGSIO(16,7)\|FINE SUSPENSION(16,4)\|CHROMIUM COMPOUND(16,3)\|COUNTER CURRENT HEAT EXCHANGE(16,1)\|DECARBONATED PELLET(16,1)\|FORSTERITE OLIVINE(16,1)\|METHANEDIONE GAS LIBERATION(16,1)\|MG2SIO(14,6)\|NA2MGSIO(14,6)\|TAILING(14,6)\|ENERGY EFFICIENCY(14,3)\|SAMPLE REACTION(14,3)\|ANHYDROUS MAGNESIUM SILICATE(14,2)\|SLURRY ADDITIVE(14,2)\|ABSORB METHANEDIONE(14,1)\|CO2 NET CONSUMER(14,1)\|CO2 SLURRY(14,1)\|DISSOLUTION BEHAVIOR(14,1)\|HEAT TRANSFER(14,1)\|HELICOIDAL TEFLON(14,1)\|MAGNETITE TRACE(14,1)\|METHANEDIONE EVAPORATION(14,1)\|MINIATURE FLOTATION CELL(14,1)\|PHOTOMETRY HYDROMAGNESITE MG(14,1)\|PREHEATER TOWER(14,1)\|SILICATE HYDROPHOBICITY(14,1)\|MAGNESIUM SILICATE WATER(13,11)\|ALKALI METAL OXIDE(13,7)\|AUTOCLAVE(13,5)\|PERICLASE(13,5)\|HUMIDITY CONDITION(13,4)\|PARTICULATE(12,4)\|POWDERED PRODUCT(12,4)\|PRODUCT RICH(12,4)\|BURNING ZONE(12,2)\|BLAINE MG(12,1)\|CARBONATE PARTICLE(12,1)\|CO2 UPTAKE(12,1)\|COMPANION PELLET(12,1)\|CONCENTRATE CO2 CONTENT(12,1)\|EFFLORESCENCE SAMPLE(12,1)\|ENHANCE NA RECYCLING(12,1)\|GROUND OLIVINE MIX(12,1)\|LASER GRANULOMETER(12,1)\|NODULE RISK(12,1)\|PERFECTLY BALANCED EQUATION(12,1)\|PRODUCT HECTORITE MANUFACTURER(12,1)\|SAMPLE DEAGGLOMERATION(12,1)\|SLURRY TEMP(12,1)\|SUSPENSION PREHEATER(12,1)\|UNREACTED ANHYDROUS COMPOUND(12,1)\|UNTREATED PELLET(12,1)\|UNTREATED RESIDUE(12,1)\|ANHYDROUS DURATION PRODUCT(11,2)\|COLORLESS SOLUTION(11,2)\|GAS ANALYZER(11,2)\|MGO EXPRESSION(11,2)\|REACTED SAMPLE PHASE CONSTITUTION(11,2)\|SI CA MG(11,2)\|SODIUM MAGNESIUM ORTHOSILICATE(11,2)\|REACTION PRODUCT(10,8)\|ALKALINE SOLUTION(10,3)\|COMBUSTION EXHAUST GAS(10,3)\|HYDROCYCLONE(10,3)\|QUENCHING(10,3)\|ANALYSIS NA2O(10,1)\|ARTINITE MG(10,1)\|CO2 10H2O(10,1)\|CO2 EMISSION(10,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(10,1)\|CURING REGIME(10,1)\|DECARBONATION REACTION(10,1)\|EARTH MANTLE COMPONENT(10,1)\|EXPERIMENT CAPTURED VOLUME(10,1)\|FERMENTATION RESIDUE GAS(10,1)\|FINE NESS(10,1)\|FINE SAND GRANULOMETRY(10,1)\|FLOTATION AID(10,1)\|INORGANIC IMPURITY(10,1)\|LAYERED DOUBLE HYDROXIDE(10,1)\|MINERAL CARBONATE(10,1)\|MOVING GRATE COOLER(10,1)\|OLIVINE SAMPLE(10,1)\|PRECIPITATED SILICA(10,1)\|R2O MOLAR RATIO(10,1)\|RAW MAGNESIUM SILICATE(10,1)\|SILICATE ANION(10,1)\|SODIUM SILICATE MILIMOLE LITER(10,1)\|SUSPENSION AGITATION(10,1)\|SYNTHETIC HECTORITE(10,1)\|UNREACTED MAGNESIUM SILICATE(10,1)\|UNREACTED PARTICLE(10,1)\|VESSEL PRESSURIZATION(10,1)\|WET CARBONATED PELLET(10,1)\|WORKING SESSION(10,1)\|R2SIO(9,5)\|SODIUM OLEATE(9,5)\|CARBOXYMETHYLCELLULOSE(9,3)\|CEMENT PLANT(8,4)\|HOT GAS(8,4)\|HYDROXY CARBONATE WATER(8,4)\|ROTARY KILN(8,4)\|ACTINOLITE(8,2)\|AMOSITE(8,2)\|AMPHIBOLE(8,2)\|ANHYDROUS SODIUM CARBONATE(8,2)\|ANTHOPHYLLITE(8,2)\|BRUCITE(8,2)\|CENTRIFUGATION(8,2)\|CHRYSOTILE(8,2)\|COMPLEX MAGNESIUM(8,2)\|ENSTATITE(8,2)\|LIQUID FILTRATE(8,2)\|MEASURED LOI DATA(8,2)\|MGO SILICA MOLAR RATIO(8,2)\|MIXED POWDER(8,2)\|PYROXENE(8,2)\|SIEVING(8,2)\|SODIUM CARBONATE POWDER(8,2)\|SYMBOL(8,2)\|TREMOLITE(8,2)\|ULTRASOUND(8,2)\|ALKALI BICARBONATE SOLUTION(8,1)\|ALKALI SOLUBLE IMPURITY(8,1)\|BASIC MAGNESIUM ORTHOSILICATE(8,1)\|BIOMASS DERIVED FUEL(8,1)\|BLUE DIODE(8,1)\|CALCULATION MATRIX(8,1)\|CARBONATABLE SOLID(8,1)\|CARBONATE ION(8,1)\|CARBONATED PRODUCT(8,1)\|CHROMIUM CONTENT(8,1)\|CO2 ATMOSPHERE(8,1)\|CO2 GRAM(8,1)\|COARSE UNREACTED SOLID(8,1)\|COMBINED CO2 QUANTITATIVE DETECTION(8,1)\|COMPRESSIVE LOAD(8,1)\|COOLED PELLET(8,1)\|CRUSHED SAMPLE(8,1)\|CRYSTALLINE COMPOUND(8,1)\|CURING CHAMBER(8,1)\|CYLINDRICAL MOLD(8,1)\|CYLINDRICAL PELLET(8,1)\|DISSOLVED ANION(8,1)\|ESTIMATED MG(8,1)\|GROUND NATURAL TALC(8,1)\|HOT NODULE HEAT(8,1)\|HOT QUENCHED SOLID(8,1)\|INCOMING COMBUSTION AIR PREHEATER(8,1)\|IRON ISOLATION(8,1)\|MAGNESIA FINE PARTICLE(8,1)\|MAGNESIUM SILICATE MINERAL(8,1)\|MAXIMUM CO2 CAPTURE(8,1)\|NATURALLY OCCURRING MINERAL(8,1)\|OUTGOING SOLID PARTICLE(8,1)\|PHASE PROBABILITY(8,1)\|PLUS MAGNESIUM(8,1)\|POROUS BED(8,1)\|POWDER SELF NODULIZE(8,1)\|PREHEATER TOP CYCLONE(8,1)\|PRESSED PELLET(8,1)\|QUALITATIVE PHASE(8,1)\|QUICK WASH(8,1)\|REACTION ESCAPE(8,1)\|REACTOR CONTENT(8,1)\|RED HE NE LASER(8,1)\|RUBBER BOWL(8,1)\|SESQUIHYDRATE(8,1)\|SILICA MOLE(8,1)\|SOLUBLE SALT(8,1)\|SORT REACTION(8,1)\|STEEL CRUCIBLE(8,1)\|SULFUR CONTENT(8,1)\|TREATED SLURRY(8,1)\|WEAK PEAK(8,1)\|XRD DATA RIETVELD ANALYSIS(8,1)\|DEIONIZED WATER(7,5)\|METHYL ISOBUTYL CARBINOL(7,5)\|ALKALI METAL CATION(7,3)\|ATMOSPHERE PRESSURE(7,3)\|DRY CONDITION(7,3)\|FE3O(7,3)\|USEFUL PRODUCT STREAM(7,3)\|NAFEO(7,2)\|SIEVE(7,2)\|4MGO FE2O(6,1)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|AIR BUBBLING(6,1)\|ALKALINE AQUEOUS SOLUTION(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANHYDROUS PRODUCT(6,1)\|ANTIGORITE(6,1)\|AQUEOUS ACID(6,1)\|AQUEOUS PHASE ICP ANALYSIS(6,1)\|AQUEOUS SOLUTION CHEMICAL SPECIES(6,1)\|ATMOSPHERIC PRESSURE CARBONATION(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|CALCINATION(6,1)\|CAO SILICA MOLAR RATIO(6,1)\|CARBONATE PRODUCT(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|CO2 MG(6,1)\|COMPRESSION MACHINE(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|CRYSTALLINE PRODUCT(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|EXCESS FERROUS SULFATE(6,1)\|FAYALITE(6,1)\|FE2SIO(6,1)\|FEO SILICA MOLAR RATIO(6,1)\|FILTER CAKE DRYING(6,1)\|\|(WO2014/082996)\|PRODUCT HECTORITE MANUFACTURER(100,1)\|AMORPHOUS SILICA PRECIPITATE(89,2)\|SILICATE MINERAL TREATMENT(78,2)\|OUTGOING HOT GAS(72,1)\|MOVING GRATE FURNACE(69,2)\|MAGNESIUM SILICATE(65,26)\|OUTGOING HOT SOLID(65,1)\|FORMULA SI(62,2)\|NEUTRALIZATION RATE(61,1)\|CARBONATED SHAPED ARTICLE(59,4)\|THEORETICAL LIMIT(59,1)\|NEUTRALIZING(56,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(55,12)\|COUNTERCURRENT HEAT EXCHANGE EFFICIENCY(54,1)\|INCOMING SOLID(54,1)\|COMPOSITION CARBONATION(53,4)\|GRATE MOVEMENT(51,2)\|GRATE LENGTH(50,1)\|NET ENERGY CONSUMPTION(47,1)\|ALKALI METAL CARBONATE(46,41)\|ALKALI METAL SILICATE(45,11)\|IRON ISOLATION(44,2)\|AMORPHOUS MAGNESIUM SILICATE WATER(42,13)\|EITELITE(41,2)\|COUNTERCURRENT HEAT EXCHANGE(40,3)\|PELLET(39,28)\|FURNACE(39,8)\|GAS LEAVING(36,3)\|MAGNESIUM OXIDE(35,13)\|MOLAR RATIO(34,11)\|MINERAL(33,9)\|INCOMING COMBUSTION AIR(33,2)\|HIGH FREQUENCY INDUCTION FURNACE(32,2)\|ALKALI METAL BICARBONATE(31,4)\|XRAY DIFFRACTION(31,4)\|MAGNESIUM OXIDE MOLAR RATIO(31,1)\|FORMULA OXIDE(30,2)\|MAGNESIUM CARBONATE COMPOUND(28,4)\|FORMULA ALKALI METAL OXIDE(28,2)\|MGC(27,18)\|UNREACTED OLIVINE(27,3)\|ALKALI METAL MAGNESIUM CARBONATE(27,1)\|BED(26,5)\|HEAT TRANSFER EFFICIENCY(25,1)\|PREHEATER CYCLONE TOWER(25,1)\|PLATINUM CRUCIBLE(23,3)\|SOLID PRODUCT(22,7)\|LAB FURNACE(22,4)\|XRAY FLUORESCENCE(22,2)\|HELICOIDAL TEFLON PADDLE(22,1)\|DECARBONATED NODULE(20,1)\|NODULE DEFORMING RISK(20,1)\|OBSCURATION STABILIZATION(20,1)\|MGSI(19,18)\|ROTARY KILN(19,3)\|EARTH CRUST(19,2)\|LASER GRANULOMETRY(19,2)\|OLIVINE SAND(19,2)\|CHROMIUM COMPOUND(18,3)\|EARTH MANTLE MAJORITY(18,1)\|FORSTERITE OLIVINE(18,1)\|MAGNESITE EXPRESSED MGO(18,1)\|SAND FINE GRANULOMETRY(18,1)\|NESQUEHONITE(16,6)\|ANHYDROUS MAGNESIUM SILICATE(16,2)\|CEMENT PLANT(16,2)\|MINERAL SILICATE(16,2)\|CARBON DIOXIDE(15,8)\|ARTINITE(15,5)\|PERICLASE(15,5)\|ENERGY EFFICIENCY(15,3)\|FINE SUSPENSION(15,3)\|CARBONATION REACTION PROGRESS(15,1)\|DISSOLUTION BEHAVIOR(15,1)\|MAGNESIA FINE PARTICLE(15,1)\|MAGNETITE TRACE(15,1)\|MINIATURE FLOTATION CELL(15,1)\|PREHEATER TOWER(15,1)\|REVEALED HYDROMAGNESITE(15,1)\|ROCK ELEMENTAL ANALYSIS(15,1)\|SILICATE HYDROPHOBICITY(15,1)\|ALKALI METAL(14,7)\|BURNING ZONE(14,2)\|DEIONIZED WATER(13,4)\|RICH PRODUCT(13,4)\|BASIC MAGNESIUM ORTHOSILICATE(13,1)\|CARBONATE PARTICLE(13,1)\|COMPANION PELLET(13,1)\|EFFLORESCENCE SAMPLE(13,1)\|IGNITION DATA(13,1)\|LASER GRANULOMETER(13,1)\|MINERAL IMPURITY(13,1)\|NA LEACHING(13,1)\|PERFECTLY BALANCED EQUATION(13,1)\|SAMPLE DEAGGLOMERATION(13,1)\|UNREACTED ANHYDROUS COMPOUND(13,1)\|UNTREATED RESIDUE(13,1)\|02 RICH COMBUSTION(12,2)\|ANHYDROUS MAGNESIUM CARBONATE(12,2)\|CARBOXYMETHYLCELLULOSE(12,2)\|COLORLESS SOLUTION(12,2)\|CRYSTALLINE CONTENT(12,2)\|ESTIMATED MG(12,2)\|GAS ANALYZER(12,2)\|MGO ANHYDROUS PRODUCT(12,2)\|REACTED SAMPLE PHASE CONSTITUTION(12,2)\|STOICHIOMETRIC RATIO(12,2)\|HYDROCYCLONE(11,3)\|ACCRETION FORMATION(11,1)\|AGITATED SUSPENSION(11,1)\|CARBONATE FUSION(11,1)\|CHROMIUM OXIDE(11,1)\|CHROMIUM SELECTIVE SEPARATION(11,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(11,1)\|DECARBONATION REACTION(11,1)\|DRIED HYDROPHASE REACTION(11,1)\|EXCESS COPPERAS(11,1)\|FERMENTATION WASTE GAS(11,1)\|FLOTATION AID(11,1)\|HE NE LASER(11,1)\|HUMAN CARCINOGEN(11,1)\|HYDROMAGNESITE CONCENTRATION(11,1)\|KG FILTER CAKE(11,1)\|LAYERED DOUBLE HYDROXIDE(11,1)\|MINERAL CARBONATE(11,1)\|MINUT ES STIRRING(11,1)\|MOVING GRATE COOLER(11,1)\|NA RECYCLING(11,1)\|NET CONSUMER(11,1)\|PELLET BED(11,1)\|POROUS GLASS FRIT(11,1)\|PRECIPITATED SILICA(11,1)\|PRESSURIZED VESSEL(11,1)\|PURE FORSTERITE(11,1)\|PURE OLIVINE SAMPLE(11,1)\|RAW MAGNESIUM SILICATE(11,1)\|RIETVELD ANALYSIS(11,1)\|SILICATE ANION(11,1)\|SLURRY ADDITIVE(11,1)\|SODIUM SILICATE MILIMOLE LITER(11,1)\|SYNTHETIC HECTORITE(11,1)\|TRISODIUM HYDROGEN DICARBONATE(11,1)\|UNREACTED MAGNESIUM SILICATE(11,1)\|UNREACTED PARTICLE(11,1)\|WATER LEACHING EFFECTIVENESS(11,1)\|WET CARBONATED PELLET(11,1)\|WORK SESSION(11,1)\|HYDROXYCARBONATE WATER(9,4)\|NAFE(9,3)\|ACTINOLITE(9,2)\|AMOSITE(9,2)\|AMPHIBOLE(9,2)\|ANTHOPHYLLITE(9,2)\|BRUCITE(9,2)\|CHRYSOTILE(9,2)\|CONTENT MG(9,2)\|DRIED FILTER(9,2)\|ENSTATITE(9,2)\|HOT GAS PASSAGE(9,2)\|HUMIDITY CONDITION(9,2)\|LIQUID FILTRATE(9,2)\|MAGNESIUM COMPLEX(9,2)\|MG CO2(9,2)\|MIXED POWDER(9,2)\|MOLAR MIXTURE RATIO(9,2)\|PYROXENE(9,2)\|SPECTROMETRY(9,2)\|SYMBOL(9,2)\|TAILING(9,2)\|TREMOLITE(9,2)\|ULTRASOUND(9,2)\|VARIABLE(9,2)\|YELLOW COLORED AQUEOUS PHASE(9,2)\|ALKALI SOLUBLE IMPURITY(9,1)\|ANHYDROUS SODIUM CARBONATE POWDER(9,1)\|AQUEOUS SUSPENSION(9,1)\|AUTOCLAVE HEATING(9,1)\|BALL MILL(9,1)\|BIOMASS DERIVED FUEL(9,1)\|BLUE DIODE(9,1)\|CARBONATABLE SOLID(9,1)\|CARBONATE ION(9,1)\|CARBONATED PRODUCT(9,1)\|CARBONATION REACTION PRODUCT(9,1)\|COARSE UNREACTED SOLID(9,1)\|COMPLETE CARBONATION(9,1)\|CONCENTRATE CONTENT(9,1)\|CRUSHED SAMPLE(9,1)\|CURING CHAMBER(9,1)\|CYLINDRICAL MOLD(9,1)\|CYLINDRICAL PELLET(9,1)\|DETECTED CAKE(9,1)\|DISSOLVED ANION MIXTURE(9,1)\|DRIED MAGNESITE PHASE REACTION(9,1)\|EITELITE PRESENCE(9,1)\|ELECTROCHEMICAL REDUCTION(9,1)\|ENERGY EXPENDITURE(9,1)\|FINAL CARBONATED(9,1)\|FUEL COMBUSTION GAS(9,1)\|GROUND NATURAL TALC(9,1)\|HOT NODULE HEAT(9,1)\|IDEALIZED OVERALL COMPOSITION MG(9,1)\|INTIMATE MIXTURE(9,1)\|IRON QUANTITY(9,1)\|MAGNESITE FORMATION(9,1)\|MAGNESIUM SILICATE MINERAL(9,1)\|MATRIX CALCULATION(9,1)\|MECHANICAL INTEGRITY MAINTENANCE(9,1)\|MECHANICAL STIRRER(9,1)\|MINERAL PREPARATION(9,1)\|MINERAL SEPARATION(9,1)\|NOMINAL COMPOSITION MG(9,1)\|OUTGOING SOLID PARTICLE(9,1)\|PELLET STRENGTH(9,1)\|PLUS MAGNESIUM(9,1)\|POROUS BED(9,1)\|PREHEATER TOP CYCLONE(9,1)\|PREHEATER WALL(9,1)\|QUALITATIVE PHASE(9,1)\|RAPID WASHING(9,1)\|REACTION ESCAPE(9,1)\|REACTION SORT(9,1)\|REMAINDER GIVING(9,1)\|RUBBER BOWL(9,1)\|SESQUIHYDRATE(9,1)\|SI DISSOLUTION(9,1)\|SILICA MOLE(9,1)\|SLURRY SAMPLE(9,1)\|SODIUM HYDROXIDE MILLIMOLE LITER(9,1)\|SOLID FILTER CAKE(9,1)\|STEEL CRUCIBLE(9,1)\|TREATED PELLET(9,1)\|TREATED SLURRY(9,1)\|VENTILATION SPEED(9,1)\|WEAK PEAK(9,1)\|WOOD CHIP(9,1)\|SIEVE(8,2)\|ALKALI METAL CATION(7,3)\|HOT WATER(7,3)\|PRESSURE ATMOSPHERE(7,3)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANTIGORITE(6,1)\|AQUEOUS PHASE ANALYSIS(6,1)\|AQUEOUS SOLUTION PH(6,1)\|ATMOSPHERE ABSOLUTE PRESSURE(6,1)\|ATMOSPHERIC PRESSURE CARBONATION(6,1)\|ATOMIC RATIO(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|BUBBLING AIR(6,1)\|CALCINATION(6,1)\|CARBON DIOXIDE EVAPORATION(6,1)\|CATALYST PRESENCE(6,1)\|CHEMICAL ADDITIVE(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|COMBUSTION EXHAUST GAS(6,1)\|COMPRESSION MACHINE(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|ELEMENT PERCENTAGE(6,1)\|EXPERIMENT SERIES(6,1)\|FACT VIRTUE(6,1)\|FAYALITE(6,1)\|FILTER CAKE DRYING(6,1)\|FILTER EXPRESSED CAKE(6,1)\|FILTER EXPRESSED MGO(6,1)\|FILTERED SOLID RESIDUE(6,1)\|FINE POWDER(6,1)\|FINE SOLID SUSPENSION(6,1)\|FINENESS(6,1)\|GARNIERITE(6,1)\|GLASS REACTOR(6,1)\|GRANULE(6,1)\|\|(JP2015536897)\|ALKALI METAL(100,81)\|ALKALI METAL CARBONATE(100,46)\|MAGNESIUM(100,16)\|MAGNESIUM OXIDE(100,16)\|ALKALI METAL BICARBONATE(100,6)\|MAGUSHIUMU SILICATE(100,3)\|SILICATE MINERAL(100,3)\|ALKALI METAL ORTHOSILICATE(100,2)\|VIRTUALIZE CARBONATE(34,1)\|SILICA MOLAR RATIO(33,3)\|SOPHORA SOIL(32,5)\|CHROMIUM TKFG(32,1)\|FINE SILICA(29,1)\|MAGNESIUM SILICATE(28,57)\|MAGNESIUM COMPLEX(28,1)\|AMORPHOUS SILICA(25,5)\|ALKALINE AQUEOUS SOLUTION(25,1)\|NEUTRALIZING(25,1)\|CRYSTALIZATION(24,1)\|MOLAR RATIO(22,15)\|MAGNESIUM SILICATE WATER(22,4)\|MOLD GOODS(22,2)\|USABLE PRODUCT(22,1)\|ALKALI METAL SILICATE(21,9)\|AMORPHOUS HYDROUS MAGNESIUM SILICATE(21,9)\|MOVING GRATE(21,2)\|LATTICE(19,1)\|SILICA COMPOUND(18,1)\|MOLDED ARTICLE(17,3)\|PELLET(16,25)\|CO2(16,22)\|MAGNESIA(16,6)\|CHEMICAL FORMULA SILICA(16,2)\|ALKALI METAL BOROHYDRIDE(16,1)\|MAGNESIUM SILICATE ROCK(15,9)\|FIRE(15,1)\|GEL FILTRATION(15,1)\|FURNACE(14,11)\|SOLID PRODUCT(14,9)\|EXPERIMENT(14,5)\|BITTERN OLIVINE(14,3)\|SIO(13,28)\|USEFUL PRODUCT STREAM(13,2)\|ALKALINE METAL CARBONATE(13,1)\|FUME NOBERUJAITO CHONDRO(13,1)\|PRODUCT STREAM(12,6)\|GROUND(11,9)\|FIBROUS SERPENTINE AMPHIBOLE(11,1)\|MAGNESIUM CARBONATE MAGNESIUM CARBONATE TRIHYDRATE(11,1)\|LABORATORY FURNACE(10,4)\|PLATINUM CRUCIBLE(10,3)\|MAGNESIUM CARBONATE HYDROXIDE HYDRATE(10,2)\|GREEN AMPHIBOLE(10,1)\|STONE EITERU SOIL(10,1)\|UNPROCESSED PELLET COMPRESSED PELLET(10,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(9,6)\|COARSE UNREACTED PARTICLE(9,1)\|FULL LENGTH(9,1)\|UNREACTED OLIVINE SAND(9,1)\|WEAK PEAK UNREACTED OLIVINE(9,1)\|CARBONATION REACTION(8,3)\|CHROMIUM COMPOUND(8,2)\|EARTH CRUST(8,2)\|GAS ANALYZER HORIBAEMIA(8,2)\|HYDROGEN DICARBONATE DIHYDRATE(8,1)\|METHANEDIONE NODULE(8,1)\|METHYLISOBUTYLCARBINOL FLOATING AID(8,1)\|OBSCURATION STABILIZATION(8,1)\|SPIRAL PADDLE STIRRER(8,1)\|VAPORIZED METHANEDIONE(8,1)\|CHEMICAL FORMULA(7,6)\|TRUE GROUND(7,3)\|ANHYDROUS MAGNESIUM SILICATE(7,2)\|CAPTURED CO2(7,2)\|NICKEL COMPOUND(7,2)\|PARTICLE SUSPENSION(7,2)\|STRAIGHT AMPHIBOLE(7,2)\|AMORPHOUS SILICA PRECIPITATION(7,1)\|BENEFICIATION SOIL(7,1)\|CARBONATION EXPERIMENT(7,1)\|CHRYSOTILE STONE(7,1)\|COMBUSTION STROKE CO2(7,1)\|DEFORMED NODULE(7,1)\|EXECUTION SUSPENSION PREHEATER(7,1)\|HEAT TRANSFER(7,1)\|HECTORITE LEE HOLDING(7,1)\|METHANEDIONE GAS LIBERATION(7,1)\|OARUNICHI STONE(7,1)\|OEITERU STONE(7,1)\|PREHEATER CYCLONE(7,1)\|ROCK UNREACTED PARTICLE(7,1)\|SILICATE HYDROPHOBICITY(7,1)\|STONE OLIVINE(7,1)\|ULTIMATUM NIGHT(7,1)\|UNREACTED ANHYDROUS COMPOUND(7,1)\|XRD QUALITATIVE PHASE(7,1)\|XRF SPECTROSCOPY(7,1)\|COMBUSTION EXHAUST GAS(6,4)\|HUMIDITY CONDITION(6,4)\|SOLID RESIDUE(6,4)\|IRON COMPOUND(6,2)\|BIOMASS DERIVED FUEL FERMENTATION(6,1)\|BUBBLE CONCENTRATE(6,1)\|DISSOLUTION BEHAVIOR(6,1)\|INORGANIC IMPURITY(6,1)\|LASER MALVERNM(6,1)\|MULTIDISTRIBUTED MATRIX(6,1)\|OLAYERED DOUBLE HYDROXIDE(6,1)\|PELLET HOT ZONE(6,1)\|POWDERED INGREDIENT(6,1)\|PREHEATER CO2(6,1)\|PRESSING IRON CRUCIBLE(6,1)\|SAMPLE DISAGGREGATION(6,1)\|SILICATE DISSOLUTION(6,1)\|SLURRY GASEOUS CO2(6,1)\|STONE LIZARD(6,1)\|TRANSPARENT AMPHIBOLE(6,1)\|REACTION PRODUCT(5,8)\|REACTOR(5,6)\|ASBESTOS(5,3)\|AUTOCLAVE(5,3)\|MAGNESIUM SILICIC ACID(5,3)\|MAGNETITE(5,3)\|BICARBONATE SALT(5,2)\|COMBUSTION ZONE(5,2)\|MAGNESIUM SILICATE MINERAL(5,2)\|MAGNESIUM SODIUM ORTHOSILICATE(5,2)\|STONE SODIUM BICARBONATE(5,2)\|SULFUR CONTENT(5,2)\|AMORPHOUS POLYESTER(5,1)\|CARBONATE DECOMPOSITION(5,1)\|CLAY MINERAL(5,1)\|CO2 DISCHARGE(5,1)\|CO2 LITER(5,1)\|EQUILIBRATED REACTION(5,1)\|ESCAPE REMAINDER(5,1)\|FINE NESS(5,1)\|FLOTATION CELL(5,1)\|GROUND OLIVINE(5,1)\|IRON OLIVINE(5,1)\|LIBERATED CO2(5,1)\|MAGNESIUM MGO(5,1)\|MEASUREMENT REPETITION(5,1)\|MINERAL CARBONATE(5,1)\|MOLDING PELLET(5,1)\|MOVING GRATE FURNACE(5,1)\|OXIDIZATION DECARBURIZATION DEGREE(5,1)\|PELLET CO2(5,1)\|PELLET COMPRESSION(5,1)\|PRINCIPAL CRYSTAL COMPOUND ALKYL(5,1)\|RUBBER BOWL(5,1)\|SLURRY ABSORPTION(5,1)\|SLURRY CO2 REACTION(5,1)\|SYNTHETIC HECTORITE(5,1)\|UNREACTED MAGNESIUM SILICATE(5,1)\|UNTREATED RESIDUE(5,1)\|ALKALI METAL OXIDE(4,7)\|CEMENT PLANT(4,4)\|ROTARY FURNACE(4,4)\|ALKALI METAL HYDROXIDE(4,3)\|ANHYDROUS SODIUM CARBONATE(4,2)\|CARBONATE COMPOUND(4,2)\|CENTRIFUGATION(4,2)\|COLORLESS SOLUTION(4,2)\|CONDITION ADOPTION(4,2)\|ENSTATITE(4,2)\|GRATING(4,2)\|MEASURED LOI DATA(4,2)\|MIXED POWDER(4,2)\|PMGO SIO(4,2)\|RICH PRODUCT(4,2)\|SIEVING(4,2)\|SODIUM CARBONATE HYDRATE POWDER(4,2)\|ALKALI BICARBONATE SOLUTION(4,1)\|ALKALI SOLUBLE IMPURITY(4,1)\|AQUEOUS SOLUTION ANION(4,1)\|ATM CO2(4,1)\|BASIC MAGNESIUM ORTHOSILICATE(4,1)\|BLUE DIODE(4,1)\|BOUND CO2(4,1)\|CALCULATION MATRIX(4,1)\|CARBONATE CO2(4,1)\|CARBONATE ION(4,1)\|CARBONATE PARTICLE(4,1)\|CHIEFLY PRODUCED STONE(4,1)\|CONTAINER PRESSURIZATION(4,1)\|CURING CHAMBER(4,1)\|FILTER CAKE DRIED CO2(4,1)\|FINE SUSPENSION(4,1)\|GAS CO2 CAPTURE(4,1)\|HOT NODULE HEAT(4,1)\|MGSIO4 PENCLASE(4,1)\|MINERAL SEPARATION(4,1)\|MOBILE COOLING(4,1)\|NATURAL TALC PRODUCTION(4,1)\|NODULE GAS(4,1)\|POROUS BED(4,1)\|QUENCHED SAMPLE(4,1)\|RESIDUE NA(4,1)\|SESQUICARBONATE WATER(4,1)\|SILICATE MINERAL TREATMENT(4,1)\|SLURRY RAPID QUENCHING(4,1)\|SODIUM SILICATE MMOLE LITER(4,1)\|SOLID MGO NA(4,1)\|SOLID PRECIPITATE CO2(4,1)\|SOLUBLE SALT(4,1)\|STIRRED SUSPENSION(4,1)\|WHITE DOT(4,1)\|WORK SESSION(4,1)\|XRD RIETVELD ANALYSIS DATA(4,1)\|XRF ANALYSIS(4,1)\|DEIONIZED WATER(3,5)\|HOT GAS(3,3)\|POWDER PRODUCTION(3,3)\|SODIUM OLEATE(3,3)\|THREE DIMENSIONAL WATER(3,3)\|DRYING CONDITION(3,2)\|PELLET BED(3,2)\|ADOPT LIQUID(3,1)\|AGGLOMERATE(3,1)\|ALKALINE SOLUTION(3,1)\|ANHYDROUS ALKALI METAL CARBONATE(3,1)\|ANHYDROUS PRODUCT(3,1)\|ANTIGORITE(3,1)\|BEAKER(3,1)\|BLOWER(3,1)\|BRUCITE(3,1)\|CHLORITE(3,1)\|CHROMIC ACID SALT(3,1)\|CHROMIUM SOLUTION(3,1)\|CLEAR GEL(3,1)\|COMPOSITION FORMULA MG(3,1)\|COMPOSITION VARIABLE(3,1)\|COMPRESSION MACHINE(3,1)\|CONCENTRATION SILICA(3,1)\|COOL SOLID(3,1)\|CYLINDRICAL MOLD(3,1)\|DECAHYDRATE(3,1)\|DEW(3,1)\|DIOPSIDE(3,1)\|DRIED SOLID XRD ANALYSIS(3,1)\|EQUILIBRIUM WATER(3,1)\|EVAPORATION PREVENTION(3,1)\|FILTRATE LIQUID(3,1)\|FINAL SAMPLE NA(3,1)\|FINE POWDER(3,1)\|FINE SOLID(3,1)\|FLOTATION SEPARATION TEST(3,1)\|FORSTERITE(3,1)\|GAMIERITE(3,1)\|GASIFICATION PROCESS CARBONATE(3,1)\|GENERATED CARBONATED PRODUCT(3,1)\|GRANULATOR(3,1)\|GRANULE(3,1)\|HEMATITE(3,1)\|HEMIHYDRATE(3,1)\|\|(CN104812468)\|SILICATE MINERAL(100,3)\|SILICATE MINERAL TREATMENT(100,1)\|FORMULA R2AN(97,3)\|MAGNESIUM SILICATE(81,64)\|AMORPHOUS MAGNESIUM SILICATE(73,7)\|ALKALI METAL CARBONATE(65,51)\|CARBONATED SHAPED ARTICLE(53,2)\|MOLAR RATIO(47,11)\|ALKALI METAL(46,74)\|MAGNESIUM ORTHOSILICATE(43,12)\|CARBONATE COMPOUND(43,2)\|ALKALI METAL SILICATE(40,8)\|ALKALI METAL BICARBONATE(39,5)\|QH2AN OXIDE(39,1)\|MAGNESIUM SILICATE HYDRATE(38,7)\|MAGNESIUM SILICATE ROCK(35,7)\|IRON ISOLATION(34,2)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(33,7)\|MAGNESIUM OXIDE(32,13)\|MAGNESITE TRIHYDRATE(27,4)\|LABORATORY FURNACE PLATINUM CRUCIBLE(24,2)\|MAGNESIUM OXIDE MOLAR RATIO(22,1)\|UNREACTED OLIVINE(20,3)\|EXTRUSION(19,2)\|CARBONATED PELLET(17,2)\|XRF SPECTROSCOPY(17,2)\|2CO3AND METHANEDIONE(15,1)\|AVAILABLEADDITIONAL CO2MAY(15,1)\|DECARBONATED NODULE(15,1)\|WET CARBONATED GRANULE(15,1)\|CHROMIUM COMPOUND(14,2)\|EARTH CRUST(14,2)\|LASER PARTICLE SIZER(14,2)\|OLIVINE SAND(14,2)\|ATMOSPHERE2ALL PELLET(13,1)\|BOUND METHANEDIONE QUANTITATIVE DETECTION(13,1)\|CO2THE NET CONSUMPTION(13,1)\|DAY2UP SKY(13,1)\|MGCO RESPECTIVELY3AND(13,1)\|MITSUBISHIMAGNESIUM ORE(13,1)\|PREHEATER CYCLONE COLUMN(13,1)\|RENDER CARBONATED PARTICLE(13,1)\|MOVING GRATE FURNACE(12,2)\|SLURRY ADDITIVE(12,2)\|ABSORB METHANEDIONE(12,1)\|ALKALI SOLUBLE IMPURITY(12,1)\|AMORPHOUS SILICA PRECIPITATE(12,1)\|CELLTHE STIRRED SUSPENSION(12,1)\|CO2UNDERGOES CURING(12,1)\|GASEOUS CO2 CAPTURE(12,1)\|LEACHING SI CA(12,1)\|METHANEDIONE EVAPORATION(12,1)\|MINERAL CHRYSOTILE(12,1)\|PREHEATER TOWER(12,1)\|SILICATE HYDROPHOBICITY(12,1)\|SODIUM CARBONATECONSISTENT EVAPORATION(12,1)\|UNREACTED ALKALI MAGNESIUM ORTHOSILICATE(12,1)\|SAMPLE REACTION(11,3)\|ASBESTOS(10,4)\|AUTOCLAVE(10,4)\|PERICLASE(10,4)\|POWDERED PRODUCT(10,4)\|WUSTITE(10,4)\|XRD ANALYSIS(10,2)\|CALCIUM FORSTERITE(10,1)\|CARBOXY METHYL CELLULOSE(10,1)\|DISSOLUTION BEHAVIOR(10,1)\|FINE MAGNESITE MG(10,1)\|GASEOUS CO2AND(10,1)\|GASEOUS CO2UP(10,1)\|HYDROMAGNESITE MG(10,1)\|LASER GRANULOMETRY(10,1)\|MAGNESIUM SILICATE RAW MEAL(10,1)\|MICRO FLOTATION(10,1)\|PELLET UPTAKE(10,1)\|PERFECTLY BALANCED EQUATION(10,1)\|RAW MEAL ANALYSIS(10,1)\|ROCK DEPOSIT(10,1)\|SAMPLE DEAGGLOMERATION(10,1)\|SODALITE NA(10,1)\|SODIUM SESQUICARBONATE DIHYDRATE(10,1)\|TRACE IMPURITY(10,1)\|UNREACTED ANHYDROUS COMPOUND(10,1)\|UNTREATED PELLET(10,1)\|UNTREATED RESIDUE(10,1)\|MAGNESIUM SILICATE WATER(9,8)\|ALKALI METAL OXIDE(9,7)\|COMBUSTION ZONE(9,2)\|MAGNESIUM SILICATE MINERAL(9,2)\|SODIUM MAGNESIUM ORTHOSILICATE(9,2)\|FE2O3AND(8,3)\|COLORLESS SOLUTION(8,2)\|ALKALI SILICATE(8,1)\|ANHYDROUS MAGNESIUM SILICATE(8,1)\|CARBONATE EVAPORATION(8,1)\|COARSE UNREACTED SOLID(8,1)\|CONCENTRATE2CO CONTENT(8,1)\|DECARBONATION REACTION(8,1)\|DISPERSIBLE POWDER(8,1)\|FERMENTATION RESIDUE GAS(8,1)\|FLOTATION AID(8,1)\|FORMULA SIO2IS(8,1)\|HYDROMAGNESITE FORMATION(8,1)\|HYDROXY SILICATE(8,1)\|INORGANIC IMPURITY(8,1)\|LAYERED DOUBLE HYDROXIDE(8,1)\|MAGNESIUM REACTION(8,1)\|MATERIAL2ADDITIONAL REACTION(8,1)\|METHANEDIONE GAS RELEASE(8,1)\|MGO SEPARATION(8,1)\|MIE MODEL(8,1)\|MINERAL CARBONATE(8,1)\|MOVING GRATE COOLER(8,1)\|OLIVE SAMPLE(8,1)\|OXIDES2THE MOLAR RATIO(8,1)\|PARTICLE SUSPENSION(8,1)\|POROUS FRIT(8,1)\|PRECIPITATED SILICA(8,1)\|PREHEATER UPPER CYCLONE(8,1)\|RAW MAGNESIUM SILICATE(8,1)\|SILICA MOLE(8,1)\|SILICATE ANION(8,1)\|SODIUM LEACHING(8,1)\|SYNTHETIC HECTORITE(8,1)\|TAILINGS2THE CONTENT(8,1)\|UNREACTED MAGNESIUM SILICATE(8,1)\|UNREACTED PARTICLE(8,1)\|VESSEL PRESSURIZATION(8,1)\|WEATHERED SAMPLE(8,1)\|XH2THE MAGNESIUM SILICATE(8,1)\|SYMBOL(7,3)\|ACTINOLITE(7,2)\|ANHYDROUS SODIUM CARBONATE(7,2)\|BRUCITE(7,2)\|CARBOXYMETHYLCELLULOSE(7,2)\|CENTRIFUGATION(7,2)\|ENSTATITE(7,2)\|GAS STREAM(7,2)\|HYDROCYCLONE(7,2)\|LIQUID FILTRATE(7,2)\|MAGNETITE(7,2)\|MEASURED LOI DATA(7,2)\|MGO SIO2IS(7,2)\|MIXED POWDER(7,2)\|OPACITY(7,2)\|PYROXENE(7,2)\|Q H2O(7,2)\|SODIUM CARBONATE SAMPLE(7,2)\|STEVENSITE(7,2)\|TREMOLITE(7,2)\|ULTRASOUND(7,2)\|3H2O(6,4)\|HOT GAS(6,4)\|MAGNESIUM CARBONATE TRIHYDRATE(6,4)\|METHYL ISOBUTYL CARBINOL(6,4)\|COUNTERCURRENT HEAT EXCHANGE(6,3)\|FOAM(6,2)\|ALKALI CARBONATE COMPOUND(6,1)\|APPLICATIONCONDITION(6,1)\|BASIC CHROMATE(6,1)\|BASIC MAGNESIUM ORTHOSILICATE(6,1)\|BLUE DIODE(6,1)\|CALCULATION MATRIX(6,1)\|CAPTURE2ASSUMING(6,1)\|CARBONATE ION(6,1)\|CARBONATED PRODUCT(6,1)\|CHROMIUM CONTENT(6,1)\|COARSE REACTED SOLID(6,1)\|COMPLEX MAGNESIUM HYDROXY(6,1)\|CRUSHED SAMPLE(6,1)\|CRYSTALLINE COMPOUND(6,1)\|CURING CHAMBER(6,1)\|CYLINDRICAL MOLD(6,1)\|CYLINDRICAL PELLET(6,1)\|DISSOLVED ANION(6,1)\|EFFLORESCENCE(6,1)\|ENHANCE NA(6,1)\|HUMIDITY CONDITION(6,1)\|ICP SOLUTION ANALYSIS(6,1)\|INCOMING COMBUSTION AIR PREHEATER(6,1)\|KILN OUTLET GAS(6,1)\|LITERS2THE GAS BUBBLE(6,1)\|MAGNESIA FINE PARTICLE(6,1)\|MAGNESIUM HYDROXY CARBONATE WATER(6,1)\|MAGNESIUM ORTHOSILICATE COMPOUND(6,1)\|MANTLE2SIO COMPONENT(6,1)\|MIXING PMGO SIO(6,1)\|NA2MGSIO4THE RATIO(6,1)\|NATURALLY OCCURRING MINERAL(6,1)\|ORDINARY STIRRER(6,1)\|PLUS MAGNESIUM(6,1)\|PREDOMINANT PHASE(6,1)\|PREDOMINANT SOLID(6,1)\|QUENCHED HOT SOLID(6,1)\|QUICK WASH(6,1)\|REACTION2TO(6,1)\|REACTOR CONTENT(6,1)\|RED HE NE LASER(6,1)\|RUBBER BOWL(6,1)\|SODALITE FORMATION(6,1)\|SOLID MICROSUSPENSION(6,1)\|SOLUBLE SALT(6,1)\|STEEL CRUCIBLE(6,1)\|SULFUR CONTENT(6,1)\|TRANSPARENT GEL(6,1)\|TREATED SLURRY(6,1)\|TRIHYDRAMAGNESITE(6,1)\|XRD DATA RIETVELD ANALYSIS(6,1)\|XRF ANALYSIS(6,1)\|4H2O(5,3)\|ALKALI METAL CATION(5,3)\|BED(5,3)\|CEMENT PLANT(5,3)\|ROTARY KILN(5,3)\|SODIUM CARBONATE HYDRATE(5,3)\|SODIUM OLEATE(5,3)\|TALC(5,3)\|USEFUL PRODUCT STREAM(5,3)\|WET CONDITION(5,3)\|2CO3MOLAR(5,1)\|2MGSIO4MGO(5,1)\|ABSORBENT(5,1)\|ACIDIC AQUEOUS SOLUTION(5,1)\|ADDED2THEREBY(5,1)\|AGITATION(5,1)\|AGITATOR SPEED(5,1)\|AIR BUBBLING(5,1)\|AMPHIBOLE(5,1)\|ANHYDROUS PRODUCT(5,1)\|ANTIGORITE(5,1)\|AQUEOUS ALKALINE SOLUTION(5,1)\|AQUEOUS PHASE ICP ANALYSIS(5,1)\|ATMOSPHERIC PRESSURE CARBONATION(5,1)\|BAR2WITHOUT(5,1)\|BASIC BICARBONATE SOLUTION(5,1)\|BEAKER(5,1)\|BIOMASS(5,1)\|BRONZITE(5,1)\|CALCINATION(5,1)\|CARBONATE RATIO(5,1)\|CHLORITE(5,1)\|CLOSED REACTOR(5,1)\|COMBUSTION EXHAUST GAS(5,1)\|COMPLEX MIXTURESYNTHETIC METAL(5,1)\|COMPRESSOR(5,1)\|CRYSTALIZATION(5,1)\|CYCLONE SEPARATOR(5,1)\|DECAHYDRATE(5,1)\|DECARBONATION DEGREE(5,1)\|DECOMPOSITION(5,1)\|DEW(5,1)\|DIOPSIDE(5,1)\|DRAINING WATER(5,1)\|DRIED FILTER(5,1)\|DRY POWDER(5,1)\|EXCESS FERROUS SULFATE(5,1)\|EXPERIMENT REACTION PRODUCT(5,1)\|FAYALITE(5,1)\|FILTERED SOLID RESIDUE(5,1)\|FINAL CARBONATED COMPOSITION REMAINS(5,1)\|FINE POWDER(5,1)\|FUEL COMBUSTION GAS(5,1)\|GARNIERITE(5,1)\|GAS ANALYZER(5,1)\|GLASS REACTOR(5,1)\|GRANULATOR(5,1)\|HEMATITE(5,1)\|HORNBLENDE(5,1)\|HOT WATER CIRCULATION(5,1)\|HOT ZONE(5,1)\|HYDRATION(5,1)\|IBALITE(5,1)\|INCORPORATION(5,1)\|\|(CN104812468)\|SILICATE MINERAL TREATMENT(100,2)\|NODULE DISTORTION(92,1)\|FORMULA R2AN(88,3)\|FORMULA SIO2AND(75,1)\|MAGNESIUM SILICATE(69,63)\|AMORPHOUS MAGNESIUM SILICATE(67,7)\|AMORPHOUS SILICA PRECIPITATE(63,2)\|ALKALI METAL CARBONATE(62,52)\|MAGNESIUM SILICATE ROCK(51,7)\|SILICATETHE ACID SALT COMPOUND(48,1)\|MAGNESIUM ORTHOSILICATE(47,14)\|FINENESS(47,1)\|SILICA PRECIPITATE(45,2)\|ALKALI METAL(43,79)\|MOLAR RATIO(43,11)\|ALKALI METAL SILICATE(41,11)\|CARBONATED SHAPED ARTICLE(40,4)\|NEUTRALIZING(39,1)\|QH2AN OXIDE(36,1)\|MAGNESIUM SILICATE HYDRATE(35,7)\|ALKALI METAL BICARBONATE(35,5)\|MAGNESIUM OXIDE(32,16)\|IRON ISOLATION(31,2)\|MOVING GRATE(30,5)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(29,8)\|METHANEDIONE(28,5)\|ACID SALT COMPOUND(26,1)\|PELLET(25,23)\|MAGNESITE TRIHYDRATE(25,4)\|USEFUL PRODUCT(23,3)\|LABORATORY FURNACE PLATINUM CRUCIBLE(22,2)\|LIQUID PRODUCT(21,1)\|FURNACE(20,8)\|MAGNESIUM OXIDE MOLAR RATIO(20,1)\|UNREACTED OLIVINE(19,3)\|STOICHIOMETRIC RATIO(18,2)\|EXTRUSION(16,3)\|REACTION DEGREE(16,2)\|CARBONATED PELLET(15,2)\|VOLUME FRACTION(15,2)\|XRF SPECTROSCOPY(15,2)\|ALKALI METAL PRODUCTION(15,1)\|2CO3AND METHANEDIONE(14,1)\|DECARBONATED NODULE(14,1)\|WET CARBONATED GRANULE(14,1)\|EARTH CRUST(13,2)\|LASER PARTICLE SIZER(13,2)\|OLIVINE SAND(13,2)\|CHROMIUM COMPOUND(12,3)\|ATMOSPHERE2ALL PELLET(12,1)\|BOUND METHANEDIONE QUANTITATIVE DETECTION(12,1)\|CHEMICAL ACTION(12,1)\|CO2THE NET CONSUMPTION(12,1)\|DAY2UP SKY(12,1)\|MGCO RESPECTIVELY3AND(12,1)\|PREHEATER CYCLONE COLUMN(12,1)\|RENDER CARBONATED PARTICLE(12,1)\|UNREACTED RAW MEAL(12,1)\|MOVING GRATE FURNACE(11,2)\|SLURRY ADDITIVE(11,2)\|WUSTITE(10,5)\|SAMPLE REACTION(10,3)\|XRD ANALYSIS(10,2)\|2MGSIO4AND MGO(10,1)\|ABSORB METHANEDIONE(10,1)\|ALKALI SOLUBLE IMPURITY(10,1)\|CO2UNDERGOES CURING(10,1)\|GASEOUS CO2 CAPTURE(10,1)\|HEAT TRANSFER(10,1)\|HORIBA EMIA(10,1)\|HOT WATERTHE HOT JACKET(10,1)\|LEACHING SI CA(10,1)\|METHANEDIONE EVAPORATION(10,1)\|MINERAL CHRYSOTILE(10,1)\|PREHEATER TOWER(10,1)\|PRODUCTONE MANUFACTURER(10,1)\|SILICATE HYDROPHOBICITY(10,1)\|SOLUBLE ONESTHE SALT(10,1)\|UNREACTED ALKALI MAGNESIUM ORTHOSILICATE(10,1)\|ASBESTOS(9,4)\|AUTOCLAVE(9,4)\|PERICLASE(9,4)\|POWDERED PRODUCT(9,4)\|CALCIUM FORSTERITE(9,1)\|CARBOXY METHYL CELLULOSE(9,1)\|DISSOLUTION BEHAVIOR(9,1)\|FINE MAGNESITE MG(9,1)\|GASEOUS CO2AND(9,1)\|GASEOUS CO2UP(9,1)\|HYDROMAGNESITE MG(9,1)\|LASER GRANULOMETRY(9,1)\|MAGNESIUM SILICATE RAW MEAL(9,1)\|MICRO FLOTATION CELL(9,1)\|PELLET UPTAKE(9,1)\|PERFECTLY BALANCED EQUATION(9,1)\|PRESERVEDTHE SAMPLE(9,1)\|RAW MEAL ANALYSIS(9,1)\|ROCK DEPOSIT(9,1)\|SAMPLE DEAGGLOMERATION(9,1)\|SODALITE NA(9,1)\|SODIUM SESQUICARBONATE DIHYDRATE(9,1)\|SUSPENSION PREHEATER(9,1)\|TRACE IMPURITY(9,1)\|UNREACTED ANHYDROUS COMPOUND(9,1)\|UNTREATED PELLET(9,1)\|UNTREATED RESIDUE(9,1)\|MAGNESIUM SILICATE WATER(8,8)\|ALKALI METAL OXIDE(8,7)\|FE2O3AND(8,3)\|MAGNETITE(8,3)\|COMBUSTION ZONE(8,2)\|MAGNESIUM SILICATE MINERAL(8,2)\|SODIUM MAGNESIUM ORTHOSILICATE(8,2)\|COUNTERCURRENT HEAT EXCHANGE(7,4)\|SYMBOL(7,3)\|COLORLESS SOLUTION(7,2)\|ALKALI SILICATE(7,1)\|ANHYDROUS MAGNESIUM SILICATE(7,1)\|CARBONATE EVAPORATION(7,1)\|COARSE UNREACTED SOLID(7,1)\|CONCENTRATE2CO CONTENT(7,1)\|DECARBONATION REACTION(7,1)\|DISPERSIBLE POWDER(7,1)\|FERMENTATION RESIDUE GAS(7,1)\|FLOTATION AID(7,1)\|FORMULA SIO2IS(7,1)\|HYDROMAGNESITE FORMATION(7,1)\|INORGANIC IMPURITY(7,1)\|LAYERED DOUBLE HYDROXIDE(7,1)\|MAGNESIUM REACTION(7,1)\|MATERIAL2ADDITIONAL REACTION(7,1)\|METHANEDIONE GAS RELEASE(7,1)\|MGO SEPARATION(7,1)\|MIE MODEL(7,1)\|MINERAL CARBONATE(7,1)\|MOVING GRATE COOLER(7,1)\|OLIVE SAMPLE(7,1)\|OXIDES2THE MOLAR RATIO(7,1)\|POROUS FRIT(7,1)\|PRECIPITATED SILICA(7,1)\|PREHEATER UPPER CYCLONE(7,1)\|RAW MAGNESIUM SILICATE(7,1)\|SILICA MOLE(7,1)\|SILICATE ANION(7,1)\|SODIUM LEACHING(7,1)\|SYNTHETIC HECTORITE(7,1)\|TAILINGS2THE CONTENT(7,1)\|UNREACTED MAGNESIUM SILICATE(7,1)\|UNREACTED PARTICLE(7,1)\|VESSEL PRESSURIZATION(7,1)\|VIRGIN MAGNESIUM SILICATE(7,1)\|WEATHERED SAMPLE(7,1)\|XH2THE MAGNESIUM SILICATE(7,1)\|3H2O(6,4)\|CEMENT PLANT(6,4)\|MAGNESIUM CARBONATE TRIHYDRATE(6,4)\|ROTARY KILN(6,4)\|ACTINOLITE(6,2)\|ANHYDROUS SODIUM CARBONATE(6,2)\|BRUCITE(6,2)\|CARBOXYMETHYLCELLULOSE(6,2)\|CENTRIFUGATION(6,2)\|ENSTATITE(6,2)\|GAS STREAM(6,2)\|HYDROCYCLONE(6,2)\|LIQUID FILTRATE(6,2)\|MEASURED LOI DATA(6,2)\|MGO SIO2IS(6,2)\|MIXED POWDER(6,2)\|MOLDING(6,2)\|NET ENERGY CONSUMPTION(6,2)\|OPACITY(6,2)\|PYROXENE(6,2)\|Q H2O(6,2)\|SODIUM CARBONATE SAMPLE(6,2)\|STEVENSITE(6,2)\|TREMOLITE(6,2)\|ULTRASOUND(6,2)\|ALKALI CARBONATE COMPOUND(6,1)\|BASIC CHROMATE(6,1)\|BASIC MAGNESIUM ORTHOSILICATE(6,1)\|BLUE DIODE(6,1)\|CALCULATION MATRIX(6,1)\|CAPTURE2ASSUMING(6,1)\|CARBONATE ION(6,1)\|CARBONATED PRODUCT(6,1)\|CHROMIUM CONTENT(6,1)\|CO2MAY(6,1)\|COARSE REACTED SOLID(6,1)\|COMPLEX MAGNESIUM HYDROXY(6,1)\|CRUSHED SAMPLE(6,1)\|CRYSTALLINE COMPOUND(6,1)\|CURING CHAMBER(6,1)\|CYLINDRICAL MOLD(6,1)\|CYLINDRICAL PELLET(6,1)\|DISSOLVED ANION(6,1)\|EFFLORESCENCE(6,1)\|ENHANCE NA(6,1)\|HOUR2THE GAS BUBBLE(6,1)\|HUMIDITY CONDITION(6,1)\|ICP SOLUTION ANALYSIS(6,1)\|INCOMING COMBUSTION AIR PREHEATER(6,1)\|INTERIM2MAY(6,1)\|KILN OUTLET GAS(6,1)\|MAGNESIA FINE PARTICLE(6,1)\|MAGNESIUM HYDROXY CARBONATE WATER(6,1)\|MAGNESIUM ORTHOSILICATE COMPOUND(6,1)\|MANTLE2SIO COMPONENT(6,1)\|MIXING PMGO SIO(6,1)\|NA2MGSIO4THE RATIO(6,1)\|NATURALLY OCCURRING MINERAL(6,1)\|ORDINARY STIRRER(6,1)\|OUTGOING HOT GAS(6,1)\|OUTGOING HOT SOLID(6,1)\|PARTICLE SUSPENSION(6,1)\|PLUS MAGNESIUM(6,1)\|PREDOMINANT PHASE(6,1)\|PREDOMINANT SOLID(6,1)\|QUENCHED HOT SOLID(6,1)\|QUICK WASH(6,1)\|REACTION2TO(6,1)\|REACTOR CONTENT(6,1)\|RED HE NE LASER(6,1)\|RUBBER BOWL(6,1)\|SAMPLEMAGNESITE(6,1)\|SODALITE FORMATION(6,1)\|SOLID MICROSUSPENSION(6,1)\|STEEL CRUCIBLE(6,1)\|STIRRED SUSPENSION(6,1)\|SULFUR CONTENT(6,1)\|TRANSPARENT GEL(6,1)\|TREATED SLURRY(6,1)\|TRIHYDRAMAGNESITE(6,1)\|XRD DATA RIETVELD ANALYSIS(6,1)\|XRF ANALYSIS(6,1)\|METHYL ISOBUTYL CARBINOL(5,4)\|4H2O(5,3)\|ALKALI METAL CATION(5,3)\|BED(5,3)\|SODIUM CARBONATE HYDRATE(5,3)\|SODIUM OLEATE(5,3)\|TALC(5,3)\|USEFUL PRODUCT STREAM(5,3)\|FOAM(5,2)\|2CO3MOLAR(4,1)\|2MGSIO4MGO(4,1)\|ABSORBENT(4,1)\|ACIDIC AQUEOUS SOLUTION(4,1)\|ADDED2THEREBY(4,1)\|AGITATION(4,1)\|AGITATOR SPEED(4,1)\|AIR BUBBLING(4,1)\|AMPHIBOLE(4,1)\|ANHYDROUS PRODUCT(4,1)\|ANTIGORITE(4,1)\|AQUEOUS ALKALINE SOLUTION(4,1)\|AQUEOUS PHASE ICP ANALYSIS(4,1)\|ATMOSPHERIC PRESSURE CARBONATION(4,1)\|BAR2WITHOUT(4,1)\|BASIC BICARBONATE SOLUTION(4,1)\|BEAKER(4,1)\|BIOMASS(4,1)\|BRONZITE(4,1)\|CALCINATION(4,1)\|CARBONATE RATIO(4,1)\|CHLORITE(4,1)\|CLOSED REACTOR(4,1)\|COMBUSTION EXHAUST GAS(4,1)\|COMPRESSOR(4,1)\|CRYSTALIZATION(4,1)\|DECAHYDRATE(4,1)\|DECARBONATION DEGREE(4,1)\|DECOMPOSITION(4,1)\|DEW(4,1)\|DIOPSIDE(4,1)\|DRAINING WATER(4,1)\|DRIED FILTER(4,1)\|DRY POWDER(4,1)\|EXCESS FERROUS SULFATE(4,1)\|EXPERIMENT REACTION PRODUCT(4,1)\|FAYALITE(4,1)\|FILTERED SOLID RESIDUE(4,1)\|FINAL CARBONATED COMPOSITION REMAINS(4,1)\|FINE POWDER(4,1)\|FUEL COMBUSTION GAS(4,1)\|GARNIERITE(4,1)\|GAS ANALYZER(4,1)\|GLASS REACTOR(4,1)\|GRANULATOR(4,1)\|HEMATITE(4,1)\|HORNBLENDE(4,1)\|HOT ZONE(4,1)\|HYDRATION(4,1)\|IBALITE(4,1)\|INCOMING SOLID(4,1)\|INCORPORATION(4,1)\|\|(AU2013351282)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,3)\|SILICATE MINERAL TREATMENT(100,3)\|MAGNESIUM SILICATE(89,63)\|LAFARGE WATERMARK INTELLECTUAL PROPERTY(88,1)\|AMORPHOUS SILICA PRECIPITATE(70,2)\|ALKALI METAL CARBONATE(65,49)\|MAGNESIUM ORTHOSILICATE(63,14)\|SILICA PRECIPITATE(62,1)\|MOLAR RATIO(56,14)\|OUTGOING HOT GAS(56,1)\|MOVING GRATE FURNACE(55,2)\|MAGNESIUM SILICATE HYDRATE(54,6)\|ALKALI METAL SILICATE(53,12)\|ALKALI METAL BICARBONATE(53,5)\|ALKALI METAL(52,76)\|OUTGOING HOT SOLID(51,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(47,12)\|CARBONATED SHAPED ARTICLE(46,4)\|NEUTRALIZING(44,1)\|MAGNESIUM OXIDE(42,16)\|INCOMING SOLID(42,1)\|USEFUL PRODUCT(38,3)\|FURNACE(37,8)\|IRON ISOLATION(35,2)\|MOVING GRATE(34,5)\|INCOMING COMBUSTION AIR(33,1)\|NET ENERGY CONSUMPTION(32,2)\|METHANEDIONE(31,5)\|COUNTERCURRENT HEAT EXCHANGE(31,3)\|TEMPERATURE ELEVATION(31,1)\|PELLET(29,24)\|EITELITE(27,6)\|CO2(25,25)\|AMBIENT TEMPERATURE(25,2)\|MAGNESIUM OXIDE MOLAR RATIO(24,1)\|PTY LTD(23,1)\|SILICON MONOXIDE(23,1)\|MGCO(21,12)\|MOLDING(21,3)\|UNREACTED OLIVINE(21,3)\|COMPLEX ALKALI METAL(21,1)\|BED(20,5)\|HEAT EXCHANGE(19,4)\|PREHEATER CYCLONE TOWER(19,1)\|OLIVINE SAND(18,3)\|PLATINUM CRUCIBLE(18,3)\|SOLID PRODUCT(17,11)\|LAB FURNACE(17,4)\|XRF SPECTROMETRY(17,2)\|PHOTOMETRY HYDROMAGNESITE MG(17,1)\|GASEOUS CO2(15,4)\|HYDROMAGNE SITE(15,3)\|EARTH CRUST(15,2)\|LASER GRANULOMETRY(15,2)\|ASBESTOS FIBRILLAR(15,1)\|DECARBONATED NODULE(15,1)\|OBSCURATION STABILIZATION(15,1)\|NESQUEHONITE(14,7)\|FINE SUSPENSION(14,4)\|CHROMIUM COMPOUND(14,3)\|COUNTER CURRENT HEAT EXCHANGE(14,1)\|DECARBONATED PELLET(14,1)\|FORSTERITE OLIVINE(14,1)\|METHANEDIONE GAS LIBERATION(14,1)\|WET CARBONATED PELLET(14,1)\|ALKALI METAL OXIDE(13,7)\|TAILING(13,6)\|ENERGY EFFICIENCY(12,3)\|SAMPLE REACTION(12,3)\|ANHYDROUS MAGNESIUM SILICATE(12,2)\|SI CA MG(12,2)\|ABSORB METHANEDIONE(12,1)\|DISSOLUTION BEHAVIOR(12,1)\|HEAT TRANSFER(12,1)\|HELICOIDAL TEFLON(12,1)\|HYDRO MAGNESITE(12,1)\|MAGNETITE TRACE(12,1)\|METHANEDIONE EVAPORATION(12,1)\|MINIATURE FLOTATION CELL(12,1)\|PREHEATER TOWER(12,1)\|SILICATE HYDROPHOBICITY(12,1)\|MAGNESIUM SILICATE WATER(11,11)\|EXPERIMENT(11,8)\|AUTOCLAVE(11,5)\|NA2MGSIA(11,5)\|PERICLASE(11,5)\|HUMIDITY CONDITION(11,4)\|BURNING ZONE(11,2)\|FE2O(10,8)\|ANHYDROUS PRODUCT(10,4)\|MG2SIO(10,4)\|PARTICULATE(10,4)\|POWDERED PRODUCT(10,4)\|PRODUCT RICH(10,4)\|R2MGSIO(10,4)\|COLORLESS SOLUTION(10,2)\|ESTIMATED MG(10,2)\|GAS ANALYZER(10,2)\|REACTED SAMPLE PHASE CONSTITUTION(10,2)\|SODIUM MAGNESIUM ORTHOSILICATE(10,2)\|CARBONATE PARTICLE(10,1)\|CO2 UPTAKE(10,1)\|COMPANION PELLET(10,1)\|CONCENTRATE CO2 CONTENT(10,1)\|EFFLORESCENCE SAMPLE(10,1)\|ENHANCE NA RECYCLING(10,1)\|GROUND OLIVINE MIX(10,1)\|LASER GRANULOMETER(10,1)\|NODULE RISK(10,1)\|PERFECTLY BALANCED EQUATION(10,1)\|PRODUCT HECTORITE MANUFACTURER(10,1)\|REACTED SAMPLE OG(10,1)\|SAMPLE DEAGGLOMERATION(10,1)\|SUSPENSION PREHEATER(10,1)\|UNREACTED ANHYDROUS COMPOUND(10,1)\|UNTREATED PELLET(10,1)\|UNTREATED RESIDUE(10,1)\|ALKALINE SOLUTION(9,3)\|COMBUSTION EXHAUST GAS(9,3)\|HYDROCYCLONE(9,3)\|MG2SIA(9,3)\|QUENCHING(9,3)\|REACTION PRODUCT(8,8)\|CARBOXYMETHYLCELLULOSE(8,3)\|ARTINITE MG(8,1)\|CHROMIUM SEPARATION(8,1)\|CO2 EMISSION(8,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(8,1)\|CURING REGIME(8,1)\|DECARBONATION REACTION(8,1)\|DRIED FILTERCAKE(8,1)\|EARTH MANTLE COMPONENT(8,1)\|FERMENTATION RESIDUE GAS(8,1)\|FINE NESS(8,1)\|FINE SAND GRANULOMETRY(8,1)\|FLOTATION AID(8,1)\|HYDROMAGNESITE FORMATION(8,1)\|INORGANIC IMPURITY(8,1)\|LAYERED DOUBLE HYDROXIDE(8,1)\|MINERAL CARBONATE(8,1)\|MOVING GRATE COOLER(8,1)\|NET CONSUMER(8,1)\|OLIVINE SAMPLE(8,1)\|PRECIPITATED SILICA(8,1)\|RAW MAGNESIUM SILICATE(8,1)\|SILICATE ANION(8,1)\|SLURRY CONC(8,1)\|SODIUM SILICATE MILIMOLE LITER(8,1)\|SUSPENSION AGITATION(8,1)\|SYNTHETIC HECTORITE(8,1)\|UNREACTED MAGNESIUM SILICATE(8,1)\|UNREACTED PARTICLE(8,1)\|VESSEL PRESSURIZATION(8,1)\|WORKING SESSION(8,1)\|SODIUM OLEATE(7,5)\|CEMENT PLANT(7,4)\|HOT GAS(7,4)\|HYDROXY CARBONATE WATER(7,4)\|R2SIO(7,4)\|ROTARY KILN(7,4)\|ACTINOLITE(7,2)\|AMOSITE(7,2)\|AMPHIBOLE(7,2)\|ANHYDROUS SODIUM CARBONATE(7,2)\|ANTHOPHYLLITE(7,2)\|BRUCITE(7,2)\|CENTRIFUGATION(7,2)\|CHRYSOTILE(7,2)\|COMPLEX MAGNESIUM(7,2)\|ENSTATITE(7,2)\|FILTER CAKE DRYING(7,2)\|LIQUID FILTRATE(7,2)\|MEASURED LOI DATA(7,2)\|MG094FE(7,2)\|MIXED POWDER(7,2)\|MR2MGSIA(7,2)\|PYROXENE(7,2)\|SIEVING(7,2)\|SODIUM CARBONATE POWDER(7,2)\|SYMBOL(7,2)\|TREMOLITE(7,2)\|ULTRASOUND(7,2)\|ALKALI BICARBONATE SOLUTION(7,1)\|ALKALI SOLUBLE IMPURITY(7,1)\|BASIC MAGNESIUM ORTHOSILICATE(7,1)\|BIOMASS DERIVED FUEL(7,1)\|BLUE DIODE(7,1)\|CALCULATION MATRIX(7,1)\|CARBONATABLE SOLID(7,1)\|CARBONATE ION(7,1)\|CARBONATED PRODUCT(7,1)\|CHROMIUM CONTENT(7,1)\|CO2 ATMOSPHERE(7,1)\|CO2 GRAM(7,1)\|COARSE UNREACTED SOLID(7,1)\|COMBINED CO2 QUANTITATIVE DETECTION(7,1)\|COMPRESSIVE LOAD(7,1)\|COOLED PELLET(7,1)\|CRUSHED SAMPLE(7,1)\|CRYSTALLINE COMPOUND(7,1)\|CRYSTALLINE CONTENT(7,1)\|CURING CHAMBER(7,1)\|CYLINDRICAL MOLD(7,1)\|CYLINDRICAL PELLET(7,1)\|DISSOLVED ANION(7,1)\|DRIED CAKE(7,1)\|EITELITE FORMATION(7,1)\|GROUND NATURAL TALC(7,1)\|HOT NODULE HEAT(7,1)\|HOT QUENCHED SOLID(7,1)\|INCOMING COMBUSTION AIR PREHEATER(7,1)\|MAGNESIA FINE PARTICLE(7,1)\|MAGNESIUM SILICATE MINERAL(7,1)\|MAXIMUM CO2 CAPTURE(7,1)\|MAXIMUM SLURRY ADDITIVE(7,1)\|NATURALLY OCCURRING MINERAL(7,1)\|OUTGOING SOLID PARTICLE(7,1)\|PHASE PROBABILITY(7,1)\|PLUS MAGNESIUM(7,1)\|POROUS BED(7,1)\|POWDER SELF NODULIZE(7,1)\|PREHEATER TOP CYCLONE(7,1)\|PRESSED PELLET(7,1)\|QUALITATIVE PHASE(7,1)\|QUICK WASH(7,1)\|REACTION ESCAPE(7,1)\|REACTOR CONTENT(7,1)\|RED HE NE LASER(7,1)\|RUBBER BOWL(7,1)\|SELFNODULIZATION(7,1)\|SESQUIHYDRATE(7,1)\|SI DISSOLUTION(7,1)\|SILICA MOLE(7,1)\|SOLUBLE SALT(7,1)\|SORT REACTION(7,1)\|STEEL CRUCIBLE(7,1)\|SULFUR CONTENT(7,1)\|TREATED SLURRY(7,1)\|WEAK PEAK(7,1)\|XRD DATA RIETVELD ANALYSIS(7,1)\|DEIONIZED WATER(6,5)\|METHYL ISOBUTYL CARBINOL(6,5)\|ALKALI METAL CATION(6,3)\|ATMOSPHERE PRESSURE(6,3)\|DRY CONDITION(6,3)\|NA2O(6,3)\|USEFUL PRODUCT STREAM(6,3)\|XH2O(6,3)\|NAFEO(6,2)\|SIEVE(6,2)\|ABSORBENT(5,1)\|ABUNDANCE(5,1)\|AIR BUBBLING(5,1)\|ALKALINE AQUEOUS SOLUTION(5,1)\|ALUMINUM(5,1)\|ANALYZING IMAGE(5,1)\|ANTIGORITE(5,1)\|AQUEOUS ACID(5,1)\|AQUEOUS PHASE ICP ANALYSIS(5,1)\|ATMOSPHERIC PRESSURE CARBONATION(5,1)\|BEAKER(5,1)\|BRONZITE(5,1)\|CALCINATION(5,1)\|CARBONATE PRODUCT(5,1)\|CHLORITE(5,1)\|CHONDRODITE(5,1)\|CLOSED REACTOR(5,1)\|COMPRESSION MACHINE(5,1)\|CONSTANT STIRRING(5,1)\|CONTENT MG(5,1)\|CRYSTALIZATION(5,1)\|CRYSTALLINE PHASE(5,1)\|CRYSTALLINE PRODUCT(5,1)\|DECAHYDRATE(5,1)\|DECARBONATION DEGREE(5,1)\|DECOMPOSITION(5,1)\|DEW(5,1)\|DIHYDRATE(5,1)\|DIOPSIDE(5,1)\|EXCESS FERROUS SULFATE(5,1)\|FAYALITE(5,1)\|FE2SIO(5,1)\|FILTER CAKE MG(5,1)\|FILTERED SOLID RESIDUE(5,1)\|FINE POWDER(5,1)\|FUEL COMBUSTION GAS(5,1)\|GARNIERITE(5,1)\|GAS STREAM(5,1)\|GLASS REACTOR(5,1)\|\|(AU2013351282)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,3)\|SILICATE MINERAL TREATMENT(100,3)\|MAGNESIUM SILICATE(89,63)\|LAFARGE WATERMARK INTELLECTUAL PROPERTY(88,1)\|AMORPHOUS SILICA PRECIPITATE(70,2)\|ALKALI METAL CARBONATE(65,49)\|MAGNESIUM ORTHOSILICATE(63,14)\|SILICA PRECIPITATE(62,1)\|MOLAR RATIO(56,14)\|OUTGOING HOT GAS(56,1)\|MOVING GRATE FURNACE(55,2)\|MAGNESIUM SILICATE HYDRATE(54,6)\|ALKALI METAL SILICATE(53,12)\|ALKALI METAL BICARBONATE(53,5)\|ALKALI METAL(52,76)\|OUTGOING HOT SOLID(51,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(47,12)\|CARBONATED SHAPED ARTICLE(46,4)\|NEUTRALIZING(44,1)\|MAGNESIUM OXIDE(42,16)\|INCOMING SOLID(42,1)\|USEFUL PRODUCT(38,3)\|FURNACE(37,8)\|IRON ISOLATION(35,2)\|MOVING GRATE(34,5)\|INCOMING COMBUSTION AIR(33,1)\|NET ENERGY CONSUMPTION(32,2)\|METHANEDIONE(31,5)\|COUNTERCURRENT HEAT EXCHANGE(31,3)\|TEMPERATURE ELEVATION(31,1)\|PELLET(29,24)\|EITELITE(27,6)\|CO2(25,25)\|AMBIENT TEMPERATURE(25,2)\|MAGNESIUM OXIDE MOLAR RATIO(24,1)\|PTY LTD(23,1)\|SILICON MONOXIDE(23,1)\|MGCO(21,12)\|MOLDING(21,3)\|UNREACTED OLIVINE(21,3)\|COMPLEX ALKALI METAL(21,1)\|BED(20,5)\|HEAT EXCHANGE(19,4)\|PREHEATER CYCLONE TOWER(19,1)\|OLIVINE SAND(18,3)\|PLATINUM CRUCIBLE(18,3)\|SOLID PRODUCT(17,11)\|LAB FURNACE(17,4)\|XRF SPECTROMETRY(17,2)\|PHOTOMETRY HYDROMAGNESITE MG(17,1)\|GASEOUS CO2(15,4)\|HYDROMAGNE SITE(15,3)\|EARTH CRUST(15,2)\|LASER GRANULOMETRY(15,2)\|ASBESTOS FIBRILLAR(15,1)\|DECARBONATED NODULE(15,1)\|OBSCURATION STABILIZATION(15,1)\|NESQUEHONITE(14,7)\|FINE SUSPENSION(14,4)\|CHROMIUM COMPOUND(14,3)\|COUNTER CURRENT HEAT EXCHANGE(14,1)\|DECARBONATED PELLET(14,1)\|FORSTERITE OLIVINE(14,1)\|METHANEDIONE GAS LIBERATION(14,1)\|WET CARBONATED PELLET(14,1)\|ALKALI METAL OXIDE(13,7)\|TAILING(13,6)\|ENERGY EFFICIENCY(12,3)\|SAMPLE REACTION(12,3)\|ANHYDROUS MAGNESIUM SILICATE(12,2)\|SI CA MG(12,2)\|ABSORB METHANEDIONE(12,1)\|DISSOLUTION BEHAVIOR(12,1)\|HEAT TRANSFER(12,1)\|HELICOIDAL TEFLON(12,1)\|HYDRO MAGNESITE(12,1)\|MAGNETITE TRACE(12,1)\|METHANEDIONE EVAPORATION(12,1)\|MINIATURE FLOTATION CELL(12,1)\|PREHEATER TOWER(12,1)\|SILICATE HYDROPHOBICITY(12,1)\|MAGNESIUM SILICATE WATER(11,11)\|EXPERIMENT(11,8)\|AUTOCLAVE(11,5)\|NA2MGSIA(11,5)\|PERICLASE(11,5)\|HUMIDITY CONDITION(11,4)\|BURNING ZONE(11,2)\|FE2O(10,8)\|ANHYDROUS PRODUCT(10,4)\|MG2SIO(10,4)\|PARTICULATE(10,4)\|POWDERED PRODUCT(10,4)\|PRODUCT RICH(10,4)\|R2MGSIO(10,4)\|COLORLESS SOLUTION(10,2)\|ESTIMATED MG(10,2)\|GAS ANALYZER(10,2)\|REACTED SAMPLE PHASE CONSTITUTION(10,2)\|SODIUM MAGNESIUM ORTHOSILICATE(10,2)\|CARBONATE PARTICLE(10,1)\|CO2 UPTAKE(10,1)\|COMPANION PELLET(10,1)\|CONCENTRATE CO2 CONTENT(10,1)\|EFFLORESCENCE SAMPLE(10,1)\|ENHANCE NA RECYCLING(10,1)\|GROUND OLIVINE MIX(10,1)\|LASER GRANULOMETER(10,1)\|NODULE RISK(10,1)\|PERFECTLY BALANCED EQUATION(10,1)\|PRODUCT HECTORITE MANUFACTURER(10,1)\|REACTED SAMPLE OG(10,1)\|SAMPLE DEAGGLOMERATION(10,1)\|SUSPENSION PREHEATER(10,1)\|UNREACTED ANHYDROUS COMPOUND(10,1)\|UNTREATED PELLET(10,1)\|UNTREATED RESIDUE(10,1)\|ALKALINE SOLUTION(9,3)\|COMBUSTION EXHAUST GAS(9,3)\|HYDROCYCLONE(9,3)\|MG2SIA(9,3)\|QUENCHING(9,3)\|REACTION PRODUCT(8,8)\|CARBOXYMETHYLCELLULOSE(8,3)\|ARTINITE MG(8,1)\|CHROMIUM SEPARATION(8,1)\|CO2 EMISSION(8,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(8,1)\|CURING REGIME(8,1)\|DECARBONATION REACTION(8,1)\|DRIED FILTERCAKE(8,1)\|EARTH MANTLE COMPONENT(8,1)\|FERMENTATION RESIDUE GAS(8,1)\|FINE NESS(8,1)\|FINE SAND GRANULOMETRY(8,1)\|FLOTATION AID(8,1)\|HYDROMAGNESITE FORMATION(8,1)\|INORGANIC IMPURITY(8,1)\|LAYERED DOUBLE HYDROXIDE(8,1)\|MINERAL CARBONATE(8,1)\|MOVING GRATE COOLER(8,1)\|NET CONSUMER(8,1)\|OLIVINE SAMPLE(8,1)\|PRECIPITATED SILICA(8,1)\|RAW MAGNESIUM SILICATE(8,1)\|SILICATE ANION(8,1)\|SLURRY CONC(8,1)\|SODIUM SILICATE MILIMOLE LITER(8,1)\|SUSPENSION AGITATION(8,1)\|SYNTHETIC HECTORITE(8,1)\|UNREACTED MAGNESIUM SILICATE(8,1)\|UNREACTED PARTICLE(8,1)\|VESSEL PRESSURIZATION(8,1)\|WORKING SESSION(8,1)\|SODIUM OLEATE(7,5)\|CEMENT PLANT(7,4)\|HOT GAS(7,4)\|HYDROXY CARBONATE WATER(7,4)\|R2SIO(7,4)\|ROTARY KILN(7,4)\|ACTINOLITE(7,2)\|AMOSITE(7,2)\|AMPHIBOLE(7,2)\|ANHYDROUS SODIUM CARBONATE(7,2)\|ANTHOPHYLLITE(7,2)\|BRUCITE(7,2)\|CENTRIFUGATION(7,2)\|CHRYSOTILE(7,2)\|COMPLEX MAGNESIUM(7,2)\|ENSTATITE(7,2)\|FILTER CAKE DRYING(7,2)\|LIQUID FILTRATE(7,2)\|MEASURED LOI DATA(7,2)\|MG094FE(7,2)\|MIXED POWDER(7,2)\|MR2MGSIA(7,2)\|PYROXENE(7,2)\|SIEVING(7,2)\|SODIUM CARBONATE POWDER(7,2)\|SYMBOL(7,2)\|TREMOLITE(7,2)\|ULTRASOUND(7,2)\|ALKALI BICARBONATE SOLUTION(7,1)\|ALKALI SOLUBLE IMPURITY(7,1)\|BASIC MAGNESIUM ORTHOSILICATE(7,1)\|BIOMASS DERIVED FUEL(7,1)\|BLUE DIODE(7,1)\|CALCULATION MATRIX(7,1)\|CARBONATABLE SOLID(7,1)\|CARBONATE ION(7,1)\|CARBONATED PRODUCT(7,1)\|CHROMIUM CONTENT(7,1)\|CO2 ATMOSPHERE(7,1)\|CO2 GRAM(7,1)\|COARSE UNREACTED SOLID(7,1)\|COMBINED CO2 QUANTITATIVE DETECTION(7,1)\|COMPRESSIVE LOAD(7,1)\|COOLED PELLET(7,1)\|CRUSHED SAMPLE(7,1)\|CRYSTALLINE COMPOUND(7,1)\|CRYSTALLINE CONTENT(7,1)\|CURING CHAMBER(7,1)\|CYLINDRICAL MOLD(7,1)\|CYLINDRICAL PELLET(7,1)\|DISSOLVED ANION(7,1)\|DRIED CAKE(7,1)\|EITELITE FORMATION(7,1)\|GROUND NATURAL TALC(7,1)\|HOT NODULE HEAT(7,1)\|HOT QUENCHED SOLID(7,1)\|INCOMING COMBUSTION AIR PREHEATER(7,1)\|MAGNESIA FINE PARTICLE(7,1)\|MAGNESIUM SILICATE MINERAL(7,1)\|MAXIMUM CO2 CAPTURE(7,1)\|MAXIMUM SLURRY ADDITIVE(7,1)\|NATURALLY OCCURRING MINERAL(7,1)\|OUTGOING SOLID PARTICLE(7,1)\|PHASE PROBABILITY(7,1)\|PLUS MAGNESIUM(7,1)\|POROUS BED(7,1)\|POWDER SELF NODULIZE(7,1)\|PREHEATER TOP CYCLONE(7,1)\|PRESSED PELLET(7,1)\|QUALITATIVE PHASE(7,1)\|QUICK WASH(7,1)\|REACTION ESCAPE(7,1)\|REACTOR CONTENT(7,1)\|RED HE NE LASER(7,1)\|RUBBER BOWL(7,1)\|SELFNODULIZATION(7,1)\|SESQUIHYDRATE(7,1)\|SI DISSOLUTION(7,1)\|SILICA MOLE(7,1)\|SOLUBLE SALT(7,1)\|SORT REACTION(7,1)\|STEEL CRUCIBLE(7,1)\|SULFUR CONTENT(7,1)\|TREATED SLURRY(7,1)\|WEAK PEAK(7,1)\|XRD DATA RIETVELD ANALYSIS(7,1)\|DEIONIZED WATER(6,5)\|METHYL ISOBUTYL CARBINOL(6,5)\|ALKALI METAL CATION(6,3)\|ATMOSPHERE PRESSURE(6,3)\|DRY CONDITION(6,3)\|NA2O(6,3)\|USEFUL PRODUCT STREAM(6,3)\|XH2O(6,3)\|NAFEO(6,2)\|SIEVE(6,2)\|ABSORBENT(5,1)\|ABUNDANCE(5,1)\|AIR BUBBLING(5,1)\|ALKALINE AQUEOUS SOLUTION(5,1)\|ALUMINUM(5,1)\|ANALYZING IMAGE(5,1)\|ANTIGORITE(5,1)\|AQUEOUS ACID(5,1)\|AQUEOUS PHASE ICP ANALYSIS(5,1)\|ATMOSPHERIC PRESSURE CARBONATION(5,1)\|BEAKER(5,1)\|BRONZITE(5,1)\|CALCINATION(5,1)\|CARBONATE PRODUCT(5,1)\|CHLORITE(5,1)\|CHONDRODITE(5,1)\|CLOSED REACTOR(5,1)\|COMPRESSION MACHINE(5,1)\|CONSTANT STIRRING(5,1)\|CONTENT MG(5,1)\|CRYSTALIZATION(5,1)\|CRYSTALLINE PHASE(5,1)\|CRYSTALLINE PRODUCT(5,1)\|DECAHYDRATE(5,1)\|DECARBONATION DEGREE(5,1)\|DECOMPOSITION(5,1)\|DEW(5,1)\|DIHYDRATE(5,1)\|DIOPSIDE(5,1)\|EXCESS FERROUS SULFATE(5,1)\|FAYALITE(5,1)\|FE2SIO(5,1)\|FILTER CAKE MG(5,1)\|FILTERED SOLID RESIDUE(5,1)\|FINE POWDER(5,1)\|FUEL COMBUSTION GAS(5,1)\|GARNIERITE(5,1)\|GAS STREAM(5,1)\|GLASS REACTOR(5,1)\|\|(KR10-2015-0088845)\|SILICATE MINERAL TREATMENT(100,2)\|DEFORMING NODULE(97,1)\|AMORPHOUS SILICA PRECIPITATE(78,1)\|MAGNESIUM SILICATE(72,61)\|AMORPHOUS MAGNESIUM SILICATE(69,6)\|ALKALI METAL CARBONATE(63,47)\|MAGNESIUM SILICATE WEIGHT(54,2)\|CO2ALKALI METAL MAGNESIUM ORTHOSILICATE(53,1)\|MOBILE GRATE(48,3)\|MAGNESIUM ORTHOSILICATE(47,13)\|SILICA PRECIPITATE(45,2)\|ALKALI METAL(43,72)\|CARBONATED SHAPED ARTICLE(43,3)\|MAGNESIUM SILICATE HYDRATE(42,16)\|REACTIVITY(42,1)\|ALKALI METAL SILICATE(41,11)\|MAGNESIUM SILICATE ROCK(39,8)\|NEUTRALIZATION RATE(39,1)\|NEUTRALIZING(39,1)\|CO2ALKALI METAL(37,1)\|HYDRATE(35,7)\|ALKALI METAL BICARBONATE(35,5)\|MAGNESIUM OXIDE(32,17)\|IRON ISOLATION(31,2)\|HUMAN CARCINOGEN(31,1)\|SILICON DIOXIDE(30,4)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(28,10)\|SIO2(27,8)\|INCINERATOR(27,6)\|HEALTH(26,1)\|ASBESTOS(24,4)\|PELLET(23,22)\|LABORATORY INCINERATOR(21,4)\|LIQUID PRODUCT(21,1)\|USEFUL PRODUCT(20,5)\|MAGNESIUM OXIDE MOLAR RATIO(20,1)\|MAGNESIUM CARBONATE COMPOUND(19,3)\|BED(18,5)\|MGO(17,20)\|PREHEATER CYCLONE TOWER(17,1)\|PLATINUM CRUCIBLE(16,3)\|VOLUME FRACTION(15,2)\|XRF SPECTROSCOPY(15,2)\|MOBILE GRATE INCINERATOR(15,1)\|DECARBONATED NODULE(14,1)\|UNREACTED OLIVINE WEAK PEAK(14,1)\|CARBONATION REACTION(13,3)\|OLIVINE SAND(13,2)\|NESQUEHONITE(12,7)\|HYDROXY CARBONATE HYDRATE(12,4)\|CHROMIUM COMPOUND(12,3)\|EARTH MANTLE(12,3)\|RENDER CARBONATED PARTICLE(12,1)\|ANHYDROUS MAGNESIUM SILICATE(11,2)\|CO2 ATM(11,2)\|GASEOUS CO2(11,2)\|HYDROCYCLONE PASSAGE(11,2)\|CARBON DIOXIDE(10,11)\|CARBOXYMETHYLCELLULOSE(10,4)\|MAGNETITE(10,4)\|FINE SUSPENSION(10,3)\|SAMPLE REACTION(10,3)\|BURNING ZONE(10,2)\|CARBONATED MOLDED ARTICLE(10,1)\|HEAT TRANSFER(10,1)\|HYDROMAGNESITE DISSOLVE(10,1)\|PREHEATER TOWER(10,1)\|SERPENTINE CRUSHED SAMPLE(10,1)\|SILICATE HYDROPHOBICITY(10,1)\|AQUEOUS SOLUTION(9,9)\|FERRICLASE(9,4)\|PARTICULATE(9,4)\|ARROW HWASALPYO(9,1)\|BULK UNREACTED ANHYDROUS COMPOUND(9,1)\|DISODIUM BICARBONATE(9,1)\|EARTH OLIVINE(9,1)\|INORGANIC IMPURITY(9,1)\|MAX CO2(9,1)\|PREDOMINANT CRYSTALLINE COMPOUND(9,1)\|RESIDUAL R2C(9,1)\|SAMPLE DEAGGLOMERATION(9,1)\|SERPENTINE CANCER(9,1)\|SI02ALKALI METAL MAGNESIUM ORTHOSILICATE(9,1)\|SILICATE ANION(9,1)\|SUSPENSION PREHEATER(9,1)\|VENTILATION FAN(9,1)\|ALKALI METAL OXIDE(8,7)\|NA2MGSI(8,3)\|SEDIMENTATION(8,3)\|ANHYDROUS MAGNESIUM CARBONATE(8,2)\|CARBONATE MELTING(8,2)\|SODIUM MAGNESIUM ORTHOSILICATE(8,2)\|TOOLIVINE(8,2)\|XRD ANALYSIS(8,2)\|REACTION PRODUCT(7,8)\|10H2THE PEAK(7,1)\|CARBONATE EVAPORATION(7,1)\|CHROMIUM SEPARATION(7,1)\|COMPOSITION MAGNESIUM SILICATE HYDRATE(7,1)\|DISPERSIBLE POWDER(7,1)\|DISSOLUTION BEHAVIOR(7,1)\|DISSOLVE MAGNESIUM SILICATE(7,1)\|FERMENTATION RESIDUE GAS(7,1)\|FINE SAND GRANULOMETRY(7,1)\|FLOATATION AID(7,1)\|IRON OLIVINE(7,1)\|LAYERED DOUBLE HYDROXIDE(7,1)\|MGCO3 ACCOUNT(7,1)\|MINERAL CARBONATE(7,1)\|MOBILE GRATE SPEED(7,1)\|MOVING GRATE FURNACE(7,1)\|NA RECYCLING(7,1)\|NET CONSUMER(7,1)\|OLIVINE SAMPLE(7,1)\|PRECIPITATED SILICA(7,1)\|RAW MAGNESIUM SILICATE(7,1)\|SLURRY ADDITIVE(7,1)\|SPIRAL TEFLON(7,1)\|SUSTAINED STIRRING(7,1)\|SYNTHETIC HECTORITE(7,1)\|UNREACTED MAGNESIUM SILICATE(7,1)\|UNREACTED PARTICLE(7,1)\|UNTREATED RESIDUE(7,1)\|VESSEL PRESSURIZATION(7,1)\|WET CARBONATED PELLET(7,1)\|WHITENED SAMPLE(7,1)\|ALKALI METAL CATION(6,4)\|CEMENT PLANT(6,4)\|COUNTERCURRENT HEAT EXCHANGE(6,4)\|FE2O(6,4)\|ROTARY KILN(6,4)\|ALKALINE SOLUTION(6,2)\|ANHYDROUS SODIUM CARBONATE(6,2)\|ANTHOPHYLLITE(6,2)\|CENTRIFUGATION(6,2)\|CHRYSOTILE(6,2)\|COLORLESS SOLUTION(6,2)\|COMPLEX MAGNESIUM(6,2)\|CRYSTALIZATION(6,2)\|GAS ANALYZER(6,2)\|LIQUID FILTRATE(6,2)\|MEASURED LOI DATA(6,2)\|MIXED POWDER(6,2)\|NET ENERGY CONSUMPTION(6,2)\|QUENCHING(6,2)\|SIEVING(6,2)\|SODIUM CARBONATE HYDRATE POWDER(6,2)\|SODIUM CARBONATE SAMPLE(6,2)\|SYMBOL(6,2)\|ULTRASOUND(6,2)\|ALKALI BICARBONATE SOLUTION(6,1)\|ALKALI SOLUBLE IMPURITY(6,1)\|AUTOCLAVE HEATING(6,1)\|BASIC MAGNESIUM ORTHOSILICATE(6,1)\|BLUE DIODE(6,1)\|CARBONATE ION(6,1)\|CARBONATED PRODUCT(6,1)\|CHROMIUM CONTENT(6,1)\|COARSE PARTIAL REACTION(6,1)\|COUNTER PELLET(6,1)\|CURE CHAMBER(6,1)\|CYLINDRICAL PELLET(6,1)\|DECARBONATION(6,1)\|DRIED FILTER CAKE(6,1)\|EFFLORESCENC(6,1)\|EFFLUENT HOT GAS(6,1)\|FAST CLEANING(6,1)\|FIRING MAGNESIUM CARBONATE(6,1)\|FLOATING CELL(6,1)\|HOT QUENCHED SOLID(6,1)\|HUMIDITY CONDITION(6,1)\|HYDRATION(6,1)\|ICP SOLUTION ANALYSIS(6,1)\|INCOMING COMBUSTION AIR PREHEATER(6,1)\|LOI LOSS(6,1)\|MAGNESIUM SILICATE MINERAL(6,1)\|MAGNESIUM SILICATE SIO2(6,1)\|NA2C03PHILADELPHIA(6,1)\|OUTGOING SOLID PARTICLE(6,1)\|PHASE LIKELIHOOD(6,1)\|POLYDISPERSITY(6,1)\|POROUS BED(6,1)\|POTASSIUM CARBONATE HYDRATE(6,1)\|PREHEATER TOP CYCLONE(6,1)\|QUALITATIVE PHASE(6,1)\|REACTED SAMPLE PHASE CONSTITUTION(6,1)\|REACTOR CONTENT(6,1)\|RED HE NE LASER(6,1)\|RESIDUAL AIR PURGING(6,1)\|RICH COMBUSTION EXHAUST GAS(6,1)\|RUBBER BOWL(6,1)\|SILICA MOLE(6,1)\|SOLID SILICA PRECIPITATE(6,1)\|SPHEROIDIZATION(6,1)\|STEEL CRUCIBLE(6,1)\|STIRRED SUSPENSION(6,1)\|SULFUR CONTENT(6,1)\|TREATED SLURRY(6,1)\|UNTREATED PELLET PAIR(6,1)\|WORKING ZONE(6,1)\|XRD DATA RIETVELD ANALYSIS(6,1)\|POWDER PRODUCTION(5,3)\|SODIUM OLEATE(5,3)\|WET CONDITION(5,3)\|ABSORB CARBON DIOXIDE(4,1)\|ABSORBENT(4,1)\|AIR BUBBLING(4,1)\|AMPHIBITE(4,1)\|ANHYDROUS PRODUCT(4,1)\|ANTIGOLITE(4,1)\|AQUEOUS ALKALI SOLUTION(4,1)\|AQUEOUS PHASE ICP ANALYSIS(4,1)\|ATMOSPHERIC PRESSURE CARBONATION(4,1)\|BEAKER(4,1)\|BICARBONATE MIXED SOLUTION(4,1)\|BRUCITE(4,1)\|CARBON DIOXIDE EVAPORATION(4,1)\|CARBONATE RATIO(4,1)\|CHILLER(4,1)\|CHLORITE(4,1)\|CHONDRODITE(4,1)\|COMPRESSION MACHINE(4,1)\|CONCENTRATE(4,1)\|CYLINDRICAL MOLD(4,1)\|DARKENING(4,1)\|DECAHYDRATE(4,1)\|DECARBOXYLATION DEGREE(4,1)\|DECOMPOSITION(4,1)\|DEW(4,1)\|DRAINING(4,1)\|EFFLUENT HOT SOLID(4,1)\|EITELITE(4,1)\|ENERGY INTENSIVE(4,1)\|ENSTATITE(4,1)\|EXCESS FERROUS SULFATE(4,1)\|EXPERIMENTAL PERIOD(4,1)\|FE2SI(4,1)\|FILTERED SOLID RESIDUE(4,1)\|FINE POWDER(4,1)\|FLOATING TEST(4,1)\|FLOTATION(4,1)\|FUEL COMBUSTION GAS(4,1)\|GARANIERITE(4,1)\|GAS STREAM(4,1)\|GLASS REACTOR(4,1)\|GRANULE(4,1)\|HEAT TREAT PELLET(4,1)\|HEMATITE(4,1)\|HEMICIDE(4,1)\|HEMIHYDRATE(4,1)\|HOT WATER CIRCULATION(4,1)\|HOT ZONE(4,1)\|IDINSITE(4,1)\|IGNITION MEASURED LOSS(4,1)\|INCOMING SOLID(4,1)\|INDUCTION COUPLED PLASMA PHOTOANALYSIS(4,1)\|KAOLIVINE(4,1)\|KILN EXHAUST GAS(4,1)\|LIBERATION(4,1)\|MAGNESIUM HYDROXIDE SEPARATION(4,1)\|MAGNESIUM SILICATE ROCK BACK(4,1)\|\|(CA2892325)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,2)\|SILICATE MINERAL TREATMENT(100,2)\|MAGNESIUM SILICATE(84,63)\|AMORPHOUS SILICA PRECIPITATE(70,2)\|MAGNESIUM ORTHOSILICATE(63,14)\|SILICA PRECIPITATE(62,1)\|ALKALI METAL CARBONATE(61,48)\|OUTGOING HOT GAS(56,1)\|MOLAR RATIO(55,15)\|MOVING GRATE FURNACE(55,2)\|MAGNESIUM SILICATE HYDRATE(54,6)\|ALKALI METAL SILICATE(53,12)\|ALKALI METAL BICARBONATE(53,5)\|FORMULA SI(51,1)\|OUTGOING HOT SOLID(51,1)\|ALKALI METAL(50,75)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(47,12)\|CARBONATED SHAPED ARTICLE(46,4)\|NEUTRALIZING(44,1)\|MAGNESIUM OXIDE(42,16)\|INCOMING SOLID(42,1)\|USEFUL PRODUCT(38,3)\|FURNACE(37,8)\|IRON ISOLATION(35,2)\|MOVING GRATE(34,5)\|INCOMING COMBUSTION AIR(33,1)\|NET ENERGY CONSUMPTION(32,2)\|METHANEDIONE(31,5)\|COUNTERCURRENT HEAT EXCHANGE(31,3)\|TEMPERATURE ELEVATION(31,1)\|PELLET(29,24)\|EITELITE(27,5)\|AMBIENT TEMPERATURE(25,2)\|MAGNESIUM OXIDE MOLAR RATIO(24,1)\|MGCO(23,21)\|XH2O(23,1)\|MOLDING(21,3)\|UNREACTED OLIVINE(21,3)\|COMPLEX ALKALI METAL(21,1)\|BED(20,5)\|HEAT EXCHANGE(19,4)\|PREHEATER CYCLONE TOWER(19,1)\|OLIVINE SAND(18,3)\|PLATINUM CRUCIBLE(18,3)\|SOLID PRODUCT(17,11)\|LAB FURNACE(17,4)\|HYDRO MAGNESITE(17,2)\|MGSIA(15,20)\|SLURRY ADDITIVE(15,3)\|LASER GRANULOMETRY(15,2)\|ASBESTOS FIBRILLAR(15,1)\|DECARBONATED NODULE(15,1)\|OBSCURATION STABILIZATION(15,1)\|NESQUEHONITE(14,7)\|FINE SUSPENSION(14,4)\|CHROMIUM COMPOUND(14,3)\|COUNTER CURRENT HEAT EXCHANGE(14,1)\|DECARBONATED PELLET(14,1)\|FORSTERITE OLIVINE(14,1)\|METHANEDIONE GAS LIBERATION(14,1)\|WET CARBONATED PELLET(14,1)\|ALKALI METAL OXIDE(13,7)\|TAILING(13,6)\|EARTH CRUST(13,2)\|SILICON MONOXIDE(12,13)\|EXPERIMENT(12,9)\|ENERGY EFFICIENCY(12,3)\|SAMPLE REACTION(12,3)\|ANHYDROUS MAGNESIUM SILICATE(12,2)\|ABSORB METHANEDIONE(12,1)\|DISSOLUTION BEHAVIOR(12,1)\|HEAT TRANSFER(12,1)\|HELICOIDAL TEFLON(12,1)\|MAGNETITE TRACE(12,1)\|METHANEDIONE EVAPORATION(12,1)\|MINIATURE FLOTATION CELL(12,1)\|PREHEATER TOWER(12,1)\|SILICATE HYDROPHOBICITY(12,1)\|XRF SPECTROMETRY(12,1)\|MAGNESIUM SILICATE WATER(11,11)\|AUTOCLAVE(11,5)\|CONCENTRATE(11,5)\|PERICLASE(11,5)\|HUMIDITY CONDITION(11,4)\|BURNING ZONE(11,2)\|ANHYDROUS PRODUCT(10,4)\|PARTICULATE(10,4)\|POWDERED PRODUCT(10,4)\|PRODUCT RICH(10,4)\|COLORLESS SOLUTION(10,2)\|ESTIMATED MG(10,2)\|GAS ANALYZER(10,2)\|REACTED SAMPLE PHASE CONSTITUTION(10,2)\|RICH COMBUSTION EXHAUST GAS(10,2)\|SODIUM MAGNESIUM ORTHOSILICATE(10,2)\|CARBONATE PARTICLE(10,1)\|COMPANION PELLET(10,1)\|EFFLORESCENCE SAMPLE(10,1)\|EITELITE NA(10,1)\|ENHANCE NA RECYCLING(10,1)\|GROUND OLIVINE MIX(10,1)\|HYDROMAGNESITE MG(10,1)\|LASER GRANULOMETER(10,1)\|NODULE RISK(10,1)\|PERFECTLY BALANCED EQUATION(10,1)\|PRODUCT HECTORITE MANUFACTURER(10,1)\|REACTED SAMPLE OG(10,1)\|SAMPLE DEAGGLOMERATION(10,1)\|SUSPENSION PREHEATER(10,1)\|UNREACTED ANHYDROUS COMPOUND(10,1)\|UNTREATED PELLET(10,1)\|UNTREATED RESIDUE(10,1)\|ALKALINE SOLUTION(9,3)\|FILTER CAKE DRYING(9,3)\|HYDROCYCLONE(9,3)\|QUENCHING(9,3)\|REACTION PRODUCT(8,8)\|CARBOXYMETHYLCELLULOSE(8,3)\|ARTINITE MG(8,1)\|CHROMIUM SEPARATION(8,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(8,1)\|CURING REGIME(8,1)\|DECARBONATION REACTION(8,1)\|DRIED FILTERCAKE(8,1)\|EARTH MANTLE COMPONENT(8,1)\|FERMENTATION RESIDUE GAS(8,1)\|FINE NESS(8,1)\|FINE SAND GRANULOMETRY(8,1)\|FLOTATION AID(8,1)\|HYDROMAGNESITE FORMATION(8,1)\|INORGANIC IMPURITY(8,1)\|LAYERED DOUBLE HYDROXIDE(8,1)\|MINERAL CARBONATE(8,1)\|MOVING GRATE COOLER(8,1)\|NET CONSUMER(8,1)\|OLIVINE SAMPLE(8,1)\|PRECIPITATED SILICA(8,1)\|QUANTITATIVE DETECTION(8,1)\|RAW MAGNESIUM SILICATE(8,1)\|SILICATE ANION(8,1)\|SLURRY CONC(8,1)\|SODIUM SILICATE MILIMOLE LITER(8,1)\|SUSPENSION AGITATION(8,1)\|SYNTHETIC HECTORITE(8,1)\|UNREACTED MAGNESIUM SILICATE(8,1)\|UNREACTED PARTICLE(8,1)\|VESSEL PRESSURIZATION(8,1)\|WORKING SESSION(8,1)\|CEMENT PLANT(7,4)\|HOT GAS(7,4)\|HYDROXY CARBONATE WATER(7,4)\|ROTARY KILN(7,4)\|SODIUM OLEATE(7,4)\|ACTINOLITE(7,2)\|AMOSITE(7,2)\|AMPHIBOLE(7,2)\|ANHYDROUS SODIUM CARBONATE(7,2)\|ANTHOPHYLLITE(7,2)\|BRUCITE(7,2)\|CENTRIFUGATION(7,2)\|CHRYSOTILE(7,2)\|COMPLEX MAGNESIUM(7,2)\|CRYSTALLINE PHASE(7,2)\|ENSTATITE(7,2)\|LIQUID FILTRATE(7,2)\|MEASURED LOI DATA(7,2)\|MG094FE(7,2)\|MIXED POWDER(7,2)\|PYROXENE(7,2)\|SIEVING(7,2)\|SODIUM CARBONATE POWDER(7,2)\|SYMBOL(7,2)\|TREMOLITE(7,2)\|ULTRASOUND(7,2)\|ALKALI BICARBONATE SOLUTION(7,1)\|ALKALI SOLUBLE IMPURITY(7,1)\|BASIC MAGNESIUM ORTHOSILICATE(7,1)\|BIOMASS DERIVED FUEL(7,1)\|BLUE DIODE(7,1)\|CALCULATION MATRIX(7,1)\|CARBONATABLE SOLID(7,1)\|CARBONATE ION(7,1)\|CARBONATED PRODUCT(7,1)\|CHROMIUM CONTENT(7,1)\|COARSE UNREACTED SOLID(7,1)\|COMPRESSIVE LOAD(7,1)\|COOLED PELLET(7,1)\|CRUSHED SAMPLE(7,1)\|CRYSTALLINE COMPOUND(7,1)\|CURING CHAMBER(7,1)\|CYLINDRICAL MOLD(7,1)\|CYLINDRICAL PELLET(7,1)\|DISSOLVED ANION(7,1)\|EITELITE FORMATION(7,1)\|FLOTATION TEST(7,1)\|GASEOUS CO2(7,1)\|GROUND NATURAL TALC(7,1)\|HOT NODULE HEAT(7,1)\|HOT QUENCHED SOLID(7,1)\|INCOMING COMBUSTION AIR PREHEATER(7,1)\|MAGNESIA FINE PARTICLE(7,1)\|MAGNESIUM SILICATE MINERAL(7,1)\|NATURALLY OCCURRING MINERAL(7,1)\|OUTGOING SOLID PARTICLE(7,1)\|PHASE PROBABILITY(7,1)\|PLUS MAGNESIUM(7,1)\|POROUS BED(7,1)\|POWDER SELF NODULIZE(7,1)\|PREHEATER TOP CYCLONE(7,1)\|PRESSED PELLET(7,1)\|QUALITATIVE PHASE(7,1)\|QUICK WASH(7,1)\|REACTION ESCAPE(7,1)\|REACTOR CONTENT(7,1)\|RED HE NE LASER(7,1)\|RUBBER BOWL(7,1)\|SELFNODULIZATION(7,1)\|SESQUIHYDRATE(7,1)\|SI DISSOLUTION(7,1)\|SILICA MOLE(7,1)\|SOLUBLE SALT(7,1)\|SORT REACTION(7,1)\|STEEL CRUCIBLE(7,1)\|SULFUR CONTENT(7,1)\|TREATED SLURRY(7,1)\|WEAK PEAK(7,1)\|XRD DATA RIETVELD ANALYSIS(7,1)\|DEIONIZED WATER(6,5)\|METHYL ISOBUTYL CARBINOL(6,5)\|ALKALI METAL CATION(6,3)\|ATMOSPHERE PRESSURE(6,3)\|DRY CONDITION(6,3)\|MGSIO(6,3)\|USEFUL PRODUCT STREAM(6,3)\|NAFEO(6,2)\|SIEVE(6,2)\|ABSORBENT(5,1)\|ABUNDANCE(5,1)\|AIR BUBBLING(5,1)\|ALKALINE AQUEOUS SOLUTION(5,1)\|ALUMINUM(5,1)\|ANALYZING IMAGE(5,1)\|ANTIGORITE(5,1)\|AQUEOUS ACID(5,1)\|AQUEOUS PHASE ICP ANALYSIS(5,1)\|ATMOSPHERIC PRESSURE CARBONATION(5,1)\|BEAKER(5,1)\|BLOCKAGE(5,1)\|BRONZITE(5,1)\|CALCINATION(5,1)\|CARBONATE PRODUCT(5,1)\|CHLORITE(5,1)\|CHONDRODITE(5,1)\|CLOSED REACTOR(5,1)\|COMPRESSION MACHINE(5,1)\|CONSTANT STIRRING(5,1)\|CRYSTALIZATION(5,1)\|CRYSTALLINE PRODUCT(5,1)\|DECAHYDRATE(5,1)\|DECARBONATION DEGREE(5,1)\|DECOMPOSITION(5,1)\|DEW(5,1)\|DIHYDRATE(5,1)\|DIOPSIDE(5,1)\|DURATIO N(5,1)\|EXCESS FERROUS SULFATE(5,1)\|FAYALITE(5,1)\|FE2SIO(5,1)\|FILTERED SOLID RESIDUE(5,1)\|FINE POWDER(5,1)\|FUEL COMBUSTION GAS(5,1)\|GARNIERITE(5,1)\|GAS STREAM(5,1)\|GLASS REACTOR(5,1)\|GRANULE(5,1)\|HEMATITE(5,1)\|HOT WATER CIRCULATION(5,1)\|	(US9631257)\|The invention claimed is:\|1. A process for the treatment of a silicate mineral, said process comprising:\| preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 600° C. to 1000° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, wherein the reaction is obtained by contacting the alkali metal carbonate compound and the magnesium silicate to each other in a solid state, and\| contacting the first composition with water to produce a second composition comprising an amorphous magnesium silicate hydrate (M-S—H).\|2. A process according to claim 1, wherein M-S—H is represented by an oxide formula in the form pMgO.SiO2.qH2O where p is from 0.5 to 2.0 and q is from 1 to 4.\|3. A process according to claim 1, wherein the magnesium silicate is a magnesium silicate in which the molar ratio of magnesium oxide to silica is from 0.5 to 3.\|4. A process according to claim 1, wherein the magnesium silicate comprises a magnesium silicate rock comprising a magnesium silicate of general composition:\|m(MgO).t(QO).SiO2xH2O\|wherein m is from 0.5 to 3, t is less than or equal to 1, x is from zero to 2, and Q represents a metal or metals other than magnesium.\|5. A process according to claim 4, wherein Q represents iron, nickel and/or chromium which process further comprises isolating an iron, nickel and/or chromium compound.\|6. A process according to claim 1, further comprising isolating or producing magnesium oxide, magnesium hydroxide or an alkali metal silicate from the second composition.\|7. A process according to claim 1, further comprising a step in which the second composition is carbonated to produce a third composition comprising a magnesium carbonate compound.\|8. A process according to the claim 7, further comprising a step in which the magnesium carbonate from the third composition is calcined to produce a fourth composition comprising magnesium oxide.\|9. A process according to claim 7, wherein the carbonation of the second composition is conducted in a second substep, after a first substep during which the second composition is formed by molding or pressing to form a shaped article, such that a carbonated shaped article is obtained.\|10. A process according to claim 1, wherein the temperature is from 800 to 1000° C.	(US9631257)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This is the U.S. National Stage of PCT/EP2013/074732, filed Nov. 26, 2013, which in turn claims priority to European Patent Application No. 12306468.5, filed Nov. 27, 2012 and European Patent Application No. 12306469.3, filed Nov. 27, 2012, the entire contents of these applications are incorporated herein by reference in their entireties.\|(US9631257)\|[0002] This invention relates to a process for the treatment of a silicate mineral. The process uses as starting material a magnesium silicate and produces an anhydrous product comprising an alkali metal magnesium orthosilicate which is then treated with water to obtain a product comprising amorphous magnesium silicate hydrate which can be subjected to further treatments to produce other products.\|[0003] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into common magnesium silicate hydrate minerals such as serpentine (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10(OH)2).\|[0004] Magnesium silicate rocks constitute an excellent source of two important elements, magnesium and silicon, in their oxide forms (MgO and SiO2). Processes to extract these two oxides from such rocks have heretofore been excessively energy-intensive and thus have not been commercialized.\|[0005] Although the magnesium silicate minerals tend to be very “unreactive,” (e.g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a “carbonate fusion”, is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analyzed by standard chemical techniques, thus allowing for total elemental analysis of the rock. The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0006] The term sodium magnesium silicate is sometimes used, in accordance with the International Nomenclature of Cosmetic Ingredients (INCI) to identify synthetic hectorites in the form of nanoparticles and which form clear gels in water. According to one manufacturer of such products hectorites have the formula (Mg5.2Li0.8)(Si8)O20(OH)4Na0.8.\|[0007] The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|[0008] The present invention accordingly provides a process for the preparation of a second composition, said process comprising the steps of:\| - preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 500 to 1200° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, and\| - contacting the first composition with water to produce the second composition comprising an amorphous magnesium silicate hydrate (M-S—H).\|[0011] M-S—H represents an amorphous magnesium silicate hydrate of variable composition. It may be represented by an oxide formula in the form pMgO.SiO2.qH2O where p is typically, from 0.5 to 2.0 and preferably from 0.6 to 1.5; and q is typically from 1 to 4.\|[0012] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate, expressed as silicon dioxide, is preferably from <4:1 to 1:4, more preferably from 3:1 to 1:3, for example 2:1 to 1:2. The ratio is most preferably about 1.\|[0013] The alkali metal is preferably potassium or, more preferably, sodium.\|[0014] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used in the process of the invention.\|[0015] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0016] The magnesium silicate used in the process of the invention is generally a mineral silicate, for example a magnesium silicate rock comprising a magnesium silicate of general composition:\|m(MgO).t(QO).SiO2.xH2O\|wherein m is from 0.5 to 3, t is less than or equal to 1, x is from zero to 2; and Q represents a metal or metals other than magnesium, (for example calcium and/or a transition group metal such as iron, chromium or nickel). Preferably, the magnesium silicate rock comprises 20% or more, more preferably 50% or more of the magnesium silicate of the general composition described hereinbefore. Preferably, when Q represents iron, nickel and/or chromium, the process according to the present invention comprises isolation of an iron, nickel and/or chromium compound\|[0017] It will be understood that the composition or formulae of minerals is often depicted in terms of the theoretical amount of oxides which they contain: the oxides are, however, not present as such in the minerals whose composition is depicted in this way.\|[0018] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc, iddingsite and hectorite. These minerals may contain substantial quantities of iron in addition to magnesium and silicon, and also significant amounts of calcium, aluminium and alkali metals,\|[0019] Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, anthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens. The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0020] The mineral silicate used in the process of the invention is preferably a magnesium silicate. The MgO/SiO2 molar ratio is preferably from 0.5 to 3, more preferably 0.65 to 2. The CaO/SiO2 molar ratio is preferably ≦0.5. The FeO/SiO2 molar ratio is preferably ≦0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≦0.2.\|[0021] The alkali metal carbonate compound used in the process of the invention may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2.2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g. chlorides, sulfates, sulphites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates or hydroxides) are present which, at the temperature used in the process of the invention, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0022] The process of the invention is preferably effected at a temperature from 600 to 1100° C., more preferably from 800 to 1000° C. Heating is generally effected for a few minutes to a few hours.\|[0023] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is solid or liquid.\|[0024] According to a feature of the invention the process is effected at a temperature below the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound.\|[0025] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as “R2O” in which R is as hereinbefore defined present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt.=140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt.=106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0026] The magnesium silicate and alkali metal carbonate compound used in the process of the present invention are preferably in particulate form or in shaped form, e.g. as pellets.\|[0027] Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the process of the invention will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of a fine sand (grain size 0.06 to 0.2 mm) or, if necessary, ground to a fine powder (grain sizes below 0.06 mm). Grain sizes greater than 0.06 mm are generally determined by sieving. Grain sizes lower than 0.06 mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0028] In one embodiment the process of the invention is conducted in a moving grate furnace. This procedure is especially suited to magnesium silicate rocks (rocks comprising mainly MgO and SiO2) in which the MgO/SiO2 molar ratio is close to or greater than 1.\|[0029] A mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in FIG. 1 of the accompanying drawings.\|[0030] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0031] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone (“burning zone”) just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1a) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate (R2CO3):\|Mg2SiO4+R2CO3MgO+R2MgSiO4+CO2↑ (1a)\|in which R is as hereinbefore defined. The more general form of this reaction can be written as in equation (1b) for m>=1 and equation 1(c) for m<1:\|m(MgO).t(QO).SiO2.xH2O+R2CO3(m−1)MgO+R2MgSiO4+tQO+CO2↑+xH2O↑ (1b)\|m(MgO).t(QO).SiO2.xH2O+R2CO3(1−m)R2SiO3+mR2MgSiO4+tQO+CO2↑+xH2O↑ (1c)\|wherein m is greater than or equal to 1 for reaction (1b) and less than or equal to 1 for reaction (1c); and Q, t and x are as hereinbefore defined. The vertical arrows ↑ indicate that the carbon dioxide gas and water vapour produced by this reaction escape from the bed and exits with the rest of the exhaust gases. Thus, ideally, the final solid product remaining in the treated pellets is an intimate mixture comprising an alkali metal magnesium orthosilicate (R2MgSiO4) and optionally either magnesium oxide (MgO, also known as periclase) or an alkali metal silicate (R2SiO3), as well as other solid products comprising the other metals (Q), especially iron, which may present as magnetite (Fe3O4) or possibly as an alkali metal ferrite (RFeO2), calcium, which may be present as silicates, chromium, which may be present as alkali metal chromates (R2CrO4), and nickel, which may be present as oxides.\|[0032] The idealized reactions depicted in equations (1a,b,c) illustrate the production of alkali metal magnesium orthosilicates plus magnesium and/or other oxides and silicates by direct reaction of a stoichiometric (i.e. 1:1R2O:SiO2) mixture of a magnesium silicate and an alkali metal carbonate.\|[0033] This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 3.4 kJ (i.e. about 0.8 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, there will be a significant net energy consumption for the overall process. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0034] In a further embodiment, the process of the invention is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln for the process of the invention which comprises a decarbonation step which produces carbon dioxide.\|[0035] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0036] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 35% of the total solids volume. However, since the reaction itself produces no liquid products (only solids and gases) at the temperatures preferably employed, the risk of the nodules deforming significantly due to melting is quite low even at far higher initial volume fractions of alkali metal carbonate as long as the heating occurs slowly enough to allow for a significant degree of reaction to occur before complete melting of the alkali metal carbonate.\|[0037] According to a further feature of the invention the process of the invention is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The nodules are then decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0038] The decarbonated and cooled pellets or nodules, comprising an alkali metal magnesium orthosilicate and optionally either magnesium oxide or an alkali metal silicate, are treated in order to separate the reaction products.\|[0039] In the process of the invention the first composition, comprising an alkali metal magnesium orthosilicate and optionally either magnesium oxide or alkali metal silicate products is contacted with water to form a second composition comprising solid amorphous magnesium silicate hydrates (and optionally solid magnesium oxide or hydroxide), together with an aqueous solution comprising alkali metal cations, hydroxide anions and silicate anions.\|[0040] The first composition as, for example pellets or nodules, is preferably quenched in an amount of water, such that the final mixture after quenching has a temperature close to, but not exceeding, about 100° C., i.e. enough to quench the solids but avoiding excessive evaporation of water. The hot quenched solids are then preferably crushed and agitated mechanically in the form of a slurry. More water may be added if necessary. Some additional heating may be necessary.\|[0041] Alternatively the treatment with water, for example in the quenching and slurry-formation process described above, can be conducted at a temperature above 100° C. if a pressurized vessel (e.g. an autoclave) is used.\|[0042] Alternatively the above quenching and slurry-formation process can be conducted at lower or ambient temperatures. Water for converting the first composition into the second composition can optionally be recycled from another part of the process.\|[0043] The objective is to separate the components of the second composition by virtue of the facts that (a) alkali metal carbonates, silicates, chromates, sulfates and oxides or hydroxides in the product will tend to dissolve readily in water; (b) alkali metal magnesium orthosilicates will tend to hydrate in hot water to release alkali metals into solution as silicates and hydroxides, the remainder giving a fine suspension of solid amorphous magnesium silicate hydrates, and (c) magnesium oxide (MgO, also known as periclase) in the sample will tend to hydrate in hot water to give magnesium hydroxide (Mg(OH)2, also known as brucite) to form a soft and easily-dispersible powder.\|[0044] The slurry may need to be agitated mechanically. Then, the liquid phase can be separated from the bulk of the unreacted alkali metal magnesium orthosilicate and other unreacted anhydrous compounds, for example by sieving, and the fine particles of magnesium hydroxide and/or amorphous magnesium silicate hydrates which pass through the sieve as a slurry may be separated from the slurry by, for example, filtering, passage through a hydrocyclone, settling and/or centrifuging. The aqueous phase after separation of the magnesium hydroxide comprises an aqueous solution of alkali metal silicates and hydroxides.\|[0045] Alternatively, the separation process may be conducted in two steps, the first step comprising a rapid washing process to remove most of the readily soluble alkali metal carbonates, silicates and hydroxides; and the second step, conducted with additional water, comprising further hydration of both the magnesium oxide and the alkali metal magnesium orthosilicate. In this two-step approach, the water temperature is preferably lower for the first step (for example lower than 60° C.) than for the second step, and an autoclave may be used for the second step if necessary.\|[0046] The overall result of the separation process described above can be summarized as follows:\|[0047] Solid products from the process of the invention, e.g. from the furnace or kiln, (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4, MgO or R2SiO3, QO, and possibly some residual R2CO3) are contacted with water to produce a second composition comprising:\| - (a) a fine suspension comprising amorphous magnesium silicate hydrates and optionally Mg(OH)2 in a highly alkaline solution rich in alkali metal silicates, hydroxides and possibly also carbonates, and\| - (b) coarse unreacted solids comprising R2MgSiO4, and optionally MgO, QO and unreacted particles of the original magnesium silicate rock (e.g. Mg2SiO4), and which separate easily by sedimentation (e.g. in a hydrocyclone) from the fine suspension.\|[0050] The fine suspension can then be further separated (e.g. by filtration) to give\| - (c) fine solids rich in amorphous magnesium silicate hydrates and optionally Mg(OH)2, and\| - (d) a solution rich in alkali metal silicates, hydroxides and possibly also carbonates, and also comprising minor amounts of alkali-soluble impurities, e.g. sulfates and chromates.\|[0053] The initial part of the reaction of the solid products in the process of the invention with water can be written qualitatively as follows, for m≧1 (equation 2a), and m≧1 (equation 2b):\|(m−1)MgO+R2MgSiO4(m−1)Mg(OH)2+“M-S—H”+2R++(OH−,H2SiO4═,CO3═) (2a)\|(1−m)R2SiO3+mR2MgSiO4“M-S—H”+2R++(OH−,H2SiO═,CO3═) (2b)\|[0054] In the above reactions, the main solid compounds produced are an amorphous magnesium silicate hydrate, “M-S—H”, of variable composition, plus, in the case where m>1, magnesium hydroxide (brucite). The alkali metals may dissolve completely in the aqueous phase as alkali metal cations (R+), and the charge of these alkali metal cations is balanced by a mixture of dissolved anions, e.g.: hydroxide (OH−), silicate (H2SiO4═) and possibly also carbonate (CO3═), present in various ratios depending on the conditions and materials used. It is to be understood that equations 2(a) and 2(b) are not perfectly balanced equations but rather are simply intended to indicate the main initial products of the reaction between the solid products of the process of the invention with water.\|[0055] In a further embodiment of the invention the alkaline solution produced in step (d) is contacted with a carbon dioxide-containing gas, for example combustion exhaust gases, to absorb carbon dioxide and yield an alkali metal carbonate, alkali metal bicarbonate or a mixture thereof, generally in solution, and (precipitated) silica.\|[0056] For example, the aqueous solution from step (d) comprising mainly alkali metal hydroxides and silicates and also some residual alkali metal carbonates is contacted with a carbon dioxide-containing gas, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. The solution rapidly absorbs CO2 from such gases to produce a solution of alkali metal carbonates and bicarbonates, and a precipitate of amorphous silica, according to the following, or similar, equations:\|CO2(gas)+2ROH(in solution)R2CO3(in solution) (3)\|CO2(gas)+R2SiO3(in solution)R2CO3(in solution)+SiO2(solid precipitate) (4)\|CO2(gas)+R2CO3(in solution)2RHCO3(in solution) (5)\|[0057] The resulting solid silica precipitate is separated from the solution, for example by filtering, passage through a hydrocyclone, settling and/or centrifuging. In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled. Additional solutes, e.g. known salts, may also be incorporated into the solution. The precipitated silica formed by reaction (4) above can be separated, washed and dried for use in various applications.\|[0058] It will be understood by mass balance that reactions (3) and (4) should in principle be able to absorb essentially all of the CO2 released by the chemical reaction occurring in the process of the invention as shown in reaction (1), but that the additional CO2 resulting from the combustion process required to heat the starting materials will require an additional reaction to absorb it completely, e.g. either a reaction such as (5), or a further reaction with another absorbent.\|[0059] The present invention thus provides a process as described hereinbefore which further comprises isolating or producing magnesium oxide, magnesium hydroxide or an alkali metal silicate from the second composition.\|[0060] In a further embodiment of the invention, the second composition comprising M-S—H is carbonated, i.e. contacted with a carbon dioxide-containing gas, preferably in the presence of water, to produce a third composition comprising a magnesium carbonate compound. The rate of this reaction can be controlled by the temperature, the pressure, the relative humidity, the presence of catalysts and/or the type of reactor used. The carbonation reaction may be represented for example by the equation:\|sCO2(gas)+pMgO.SiO2.qH2Os“MgCO3”+(p−s)MgO.SiO2.q′H2O (6)\|[0061] The first product of this carbonation reaction, shown above as “MgCO3” may be either a simple magnesium carbonate, such as magnesite (MgCO3) or nesquehonite (MgCO3.3H2O), or a complex magnesium hydroxy-carbonate hydrate such as hydromagnesite (Mg(OH)2.4MgCO3.4H2O), or artinite (Mg(OH)2.MgCO3.3H2O), depending on the conditions employed. The second product of this reaction, shown above as “(p−s)MgO.SiO2.q′H2O” represents either an amorphous magnesium silicate hydrate with a lower magnesium/silicon ratio (p−s) than that (p) of the starting magnesium silicate hydrate; or, in the case where p=s, it represents simply a (hydrated) amorphous silica.\|[0062] In a further embodiment of the invention the coarse, partially reacted solids separated from the reaction products in step 1(b) above comprise mainly unreacted magnesium silicate (for example, Mg2SiO4) mixed with some intermediate products (for example, Na2MgSiO4). These can be dried and recycled to be mixed with additional raw magnesium silicate starting material for feeding back into the process. It will be understood that drying should be accomplished in an energy-efficient manner, e.g. first by drainage and then by use of waste heat from the furnace or other sources.\|[0063] According to a further feature of the invention all of the solid products from the process of the invention, e.g. from the furnace or kiln (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4 and MgO or R2SiO3 and/or QO, and possibly some residual R2CO3) are ground together with water to produce a suspension or slurry which is then contacted with a gas containing carbon dioxide, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. During this treatment, in addition to the other reactions described above, (e.g. in equations (2), (3), (4), (5) and (6)), the alkali metal magnesium orthosilicate compound can also react directly with CO2 as indicated by equations (7) and (8) below:\|R2MgSiO4+2CO2MgCO3(solid)+SiO2(solid)+R2CO3(in solution) (7)\|or, alternatively, making use of an alkali bicarbonate solution to achieve the same reaction:\|R2MgSiO4+4RHCO3MgCO3(solid)+SiO2(solid)+3R2CO3(in solution) (8)\|[0064] The alkali metal bicarbonate RHCO3 used in reaction (8) may be formed by the reaction of alkali metal carbonate solution R2CO3 produced in reaction (7) with carbon dioxide, as shown in equation (5).\|[0065] Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300° C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eitelite, Na2CO3.MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|[0066] These types of reaction are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid products. The magnesium carbonate solid produced can be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3.3H2O), or a complex magnesium hydroxy-carbonate hydrate, such as hydromagnesite (Mg(OH)2.4MgCO3.4H2O), or artinite (Mg(OH)2.MgCO3.3H2O), depending on the conditions and starting materials. The silica solid produced can be either a simple amorphous silica or a more complex mixed metal hydroxy-silicate such as an amorphous magnesium silicate hydrate (“M-S—H”). The alkali metal carbonate or bicarbonate solutions resulting from complete carbonation as shown in reactions (3), (4), (5), (7) and (8) can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and then recycled to the start of the process. The solid mixture of magnesium carbonates and silica produced by these reactions is one of the final products of the overall process and, after washing if necessary to recover as much as possible of the soluble alkali metal salts, can be separated for disposal or for use in other processes.\|[0067] The overall object of the process is to convert magnesium silicate rock into useful industrial products with low overall CO2 emissions. A further benefit of the process is to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable mineral carbonate which comprises a magnesium carbonate compound. Below are some examples of some different ways in which the process can be used:\|[0068] Starting with a magnesium silicate rock of composition m(MgO).t(QO).SiO2.xH2O, and recycling substantially all of the alkali metal (R) compounds used back into the process, at least two separate major product streams can be secured from amongst the following:\| - (i) Products rich in magnesium oxide or hydroxide (MgO or Mg(OH)2)\| - (ii) Products rich in amorphous silica (SiO2)\| - (iii) Products rich in amorphous magnesium silicate hydrates (M-S—H)\| - (iv) Products rich in magnesium carbonate compounds, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3, also known as magnesite); or magnesium carbonate trihydrate (MgCO3.3H2O, also known as nesquehonite); or magnesium hydroxy-carbonate hydrate, such as\|[0073] (Mg(OH)2.4MgCO3.4H2O), also known as hydromagnesite, or (Mg(OH)2.MgCO3.3H2O), also known as artinite.\|[0074] Improved separation of the above major solid product streams can also be achieved by the application of other known mineral separation techniques such as, for example, flotation. Such flotation techniques can be effected using flotation aids including sodium oleate, carboxymethylcellulose and methyl isobutyl carbinol.\|[0075] To the extent that CO2 is produced by the combustion of fuels used in the process, e.g. to heat the kiln or furnace, or to dry materials, this CO2 can be captured in the process in the form of product (iv) listed above, by using a treatment process based on the reactions shown above. To the extent that the process is energy-efficient, the aforesaid CO2 produced by the combustion of fuels used in the process, even if substantially completely captured by reactions of the sort shown, for example, in equations (3), (4) and (5), will generally not be sufficient to convert all of the magnesium in the process to product stream (iv), leaving some of the magnesium available for the production of product streams (i) and (iii). However, in another embodiment of the process, additional CO2 can be obtained from other sources and included in the treatment process and thus captured. In such a case, it is possible to operate the process in such a way that product stream (i) is not produced, but the process itself becomes a net consumer of CO2. Moreover, it is also possible to operate the process without separating any of the product streams, so that the only product stream produced is a mixture of some or all of the above product streams\|[0076] In a further approach, the process uses the same magnesium silicate raw material as shown above, but in this case, not all of the alkali metal-rich products of the process are recycled within the process. It is therefore possible to have one or more additional product streams as well as those already listed above. For example, one very useful product stream is an alkali metal silicate, (R2SiO3), either in the form of an alkaline aqueous solution also containing alkali metal hydroxides and/or carbonates, or as a solid product, (for example, obtained by evaporation and/or crystallization).\|[0077] According to a feature of the invention the process further comprises carbonation of the second composition, e.g. by treatment with gases containing CO2, to produce a third composition comprising a magnesium carbonate, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3), also known as magnesite; or magnesium carbonate trihydrate (MgCO3.3H2O), also known as nesquehonite; or magnesium hydroxy-carbonate hydrates, such as (Mg(OH)2.4MgCO3.4H2O), also known as hydromagnesite, or (Mg(OH)2.MgCO3.3H2O), also known as artinite.\|[0078] According to a further feature of the invention, the process further comprises conducting the carbonation of the second composition as described in the preceding paragraph, but where the second composition is first formed by moulding or pressing to form a shaped article, such that the resulting final carbonated composition retains the form of the shaped article but is further hardened by the formation of magnesium carbonates in situ. The present invention thus provides a process as described hereinbefore, in which the carbonation of the second composition is conducted in a second step, after a first step during which the second composition is formed by moulding or pressing to form a shaped article, such that a carbonated shaped article is obtained.\|[0079] The present invention further provides a carbonated shaped article obtained by the process as described hereinbefore.\|[0080] According to a further feature of the invention the process further comprises calcining the magnesium carbonate from the third composition to produce a fourth composition comprising magnesium oxide.\|[0081] The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|[0082] Another useful product stream is rich in transition metal oxides, for example iron oxides such as magnetite (Fe3O4), and which may also contain significant amounts of chromium and/or nickel oxides. These oxides can be concentrated by flotation and/or magnetic separation.\|[0083] Another useful product stream is an alkaline solution containing chromates, which can be treated with a reducing agent and pH control (or by electrochemical reduction) to separate relatively pure chromium oxides, or even chromium metal; for example:\|R2CrO4(aqueous solution)+(reducing agent)Cr(OH)3(solid precipitate)\|[0084] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0085] The term “pellets” as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0086] Particle size distribution when measured by laser granulometry is measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He—Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.\|[0087] The apparatus is checked before each working session by means of a standard sample (Sifraco 010 silica) for which the particle size distribution is known.\|[0088] Measurements are performed with the following parameters: pump speed 2300 rpm and stirrer speed 800 rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30 s (for possible air bubbles to clear), a measurement is carried out for 15 s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0089] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0090] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R, Q, m, t, x and, p are as initially defined.\|[0091] The following non-limiting Examples illustrate embodiments of the invention.\|[0092] The following abbreviations and notations are used:\| - XRF X-ray fluorescence\| - XRD X-ray diffraction\| - ICP Inductively-Coupled Plasma Photometry\| - Hydromagnesite Mg(OH)2.4MgCO3.4H2O\| - Artinite Mg(OH)2.MgCO3.3H2O\| - Eitelite Na2CO3.Mg(CO3)\| - LOI Loss on ignition	(US9631257)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This is the U.S. National Stage of PCT/EP2013/074732, filed Nov. 26, 2013, which in turn claims priority to European Patent Application No. 12306468.5, filed Nov. 27, 2012 and European Patent Application No. 12306469.3, filed Nov. 27, 2012, the entire contents of these applications are incorporated herein by reference in their entireties.\|(US9631257)\|[0002] This invention relates to a process for the treatment of a silicate mineral. The process uses as starting material a magnesium silicate and produces an anhydrous product comprising an alkali metal magnesium orthosilicate which is then treated with water to obtain a product comprising amorphous magnesium silicate hydrate which can be subjected to further treatments to produce other products.\|[0003] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into common magnesium silicate hydrate minerals such as serpentine (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10(OH)2).\|[0004] Magnesium silicate rocks constitute an excellent source of two important elements, magnesium and silicon, in their oxide forms (MgO and SiO2). Processes to extract these two oxides from such rocks have heretofore been excessively energy-intensive and thus have not been commercialized.\|[0005] Although the magnesium silicate minerals tend to be very “unreactive,” (e.g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a “carbonate fusion”, is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analyzed by standard chemical techniques, thus allowing for total elemental analysis of the rock. The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0006] The term sodium magnesium silicate is sometimes used, in accordance with the International Nomenclature of Cosmetic Ingredients (INCI) to identify synthetic hectorites in the form of nanoparticles and which form clear gels in water. According to one manufacturer of such products hectorites have the formula (Mg5.2Li0.8)(Si8)O20(OH)4Na0.8.\|[0007] The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|[0008] The present invention accordingly provides a process for the preparation of a second composition, said process comprising the steps of:\| - preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 500 to 1200° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, and\| - contacting the first composition with water to produce the second composition comprising an amorphous magnesium silicate hydrate (M-S—H).\|[0011] M-S—H represents an amorphous magnesium silicate hydrate of variable composition. It may be represented by an oxide formula in the form pMgO.SiO2.qH2O where p is typically, from 0.5 to 2.0 and preferably from 0.6 to 1.5; and q is typically from 1 to 4.\|[0012] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate, expressed as silicon dioxide, is preferably from <4:1 to 1:4, more preferably from 3:1 to 1:3, for example 2:1 to 1:2. The ratio is most preferably about 1.\|[0013] The alkali metal is preferably potassium or, more preferably, sodium.\|[0014] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used in the process of the invention.\|[0015] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0016] The magnesium silicate used in the process of the invention is generally a mineral silicate, for example a magnesium silicate rock comprising a magnesium silicate of general composition:\|m(MgO).t(QO).SiO2.xH2O\|wherein m is from 0.5 to 3, t is less than or equal to 1, x is from zero to 2; and Q represents a metal or metals other than magnesium, (for example calcium and/or a transition group metal such as iron, chromium or nickel). Preferably, the magnesium silicate rock comprises 20% or more, more preferably 50% or more of the magnesium silicate of the general composition described hereinbefore. Preferably, when Q represents iron, nickel and/or chromium, the process according to the present invention comprises isolation of an iron, nickel and/or chromium compound\|[0017] It will be understood that the composition or formulae of minerals is often depicted in terms of the theoretical amount of oxides which they contain: the oxides are, however, not present as such in the minerals whose composition is depicted in this way.\|[0018] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc, iddingsite and hectorite. These minerals may contain substantial quantities of iron in addition to magnesium and silicon, and also significant amounts of calcium, aluminium and alkali metals,\|[0019] Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, anthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens. The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0020] The mineral silicate used in the process of the invention is preferably a magnesium silicate. The MgO/SiO2 molar ratio is preferably from 0.5 to 3, more preferably 0.65 to 2. The CaO/SiO2 molar ratio is preferably ≦0.5. The FeO/SiO2 molar ratio is preferably ≦0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≦0.2.\|[0021] The alkali metal carbonate compound used in the process of the invention may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2.2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g. chlorides, sulfates, sulphites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates or hydroxides) are present which, at the temperature used in the process of the invention, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0022] The process of the invention is preferably effected at a temperature from 600 to 1100° C., more preferably from 800 to 1000° C. Heating is generally effected for a few minutes to a few hours.\|[0023] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is solid or liquid.\|[0024] According to a feature of the invention the process is effected at a temperature below the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound.\|[0025] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as “R2O” in which R is as hereinbefore defined present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt.=140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt.=106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0026] The magnesium silicate and alkali metal carbonate compound used in the process of the present invention are preferably in particulate form or in shaped form, e.g. as pellets.\|[0027] Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the process of the invention will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of a fine sand (grain size 0.06 to 0.2 mm) or, if necessary, ground to a fine powder (grain sizes below 0.06 mm). Grain sizes greater than 0.06 mm are generally determined by sieving. Grain sizes lower than 0.06 mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0028] In one embodiment the process of the invention is conducted in a moving grate furnace. This procedure is especially suited to magnesium silicate rocks (rocks comprising mainly MgO and SiO2) in which the MgO/SiO2 molar ratio is close to or greater than 1.\|[0029] A mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in FIG. 1 of the accompanying drawings.\|[0030] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0031] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone (“burning zone”) just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1a) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate (R2CO3):\|Mg2SiO4+R2CO3MgO+R2MgSiO4+CO2↑ (1a)\|in which R is as hereinbefore defined. The more general form of this reaction can be written as in equation (1b) for m>=1 and equation 1(c) for m<1:\|m(MgO).t(QO).SiO2.xH2O+R2CO3(m−1)MgO+R2MgSiO4+tQO+CO2↑+xH2O↑ (1b)\|m(MgO).t(QO).SiO2.xH2O+R2CO3(1−m)R2SiO3+mR2MgSiO4+tQO+CO2↑+xH2O↑ (1c)\|wherein m is greater than or equal to 1 for reaction (1b) and less than or equal to 1 for reaction (1c); and Q, t and x are as hereinbefore defined. The vertical arrows ↑ indicate that the carbon dioxide gas and water vapour produced by this reaction escape from the bed and exits with the rest of the exhaust gases. Thus, ideally, the final solid product remaining in the treated pellets is an intimate mixture comprising an alkali metal magnesium orthosilicate (R2MgSiO4) and optionally either magnesium oxide (MgO, also known as periclase) or an alkali metal silicate (R2SiO3), as well as other solid products comprising the other metals (Q), especially iron, which may present as magnetite (Fe3O4) or possibly as an alkali metal ferrite (RFeO2), calcium, which may be present as silicates, chromium, which may be present as alkali metal chromates (R2CrO4), and nickel, which may be present as oxides.\|[0032] The idealized reactions depicted in equations (1a,b,c) illustrate the production of alkali metal magnesium orthosilicates plus magnesium and/or other oxides and silicates by direct reaction of a stoichiometric (i.e. 1:1R2O:SiO2) mixture of a magnesium silicate and an alkali metal carbonate.\|[0033] This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 3.4 kJ (i.e. about 0.8 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, there will be a significant net energy consumption for the overall process. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0034] In a further embodiment, the process of the invention is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln for the process of the invention which comprises a decarbonation step which produces carbon dioxide.\|[0035] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0036] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 35% of the total solids volume. However, since the reaction itself produces no liquid products (only solids and gases) at the temperatures preferably employed, the risk of the nodules deforming significantly due to melting is quite low even at far higher initial volume fractions of alkali metal carbonate as long as the heating occurs slowly enough to allow for a significant degree of reaction to occur before complete melting of the alkali metal carbonate.\|[0037] According to a further feature of the invention the process of the invention is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The nodules are then decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0038] The decarbonated and cooled pellets or nodules, comprising an alkali metal magnesium orthosilicate and optionally either magnesium oxide or an alkali metal silicate, are treated in order to separate the reaction products.\|[0039] In the process of the invention the first composition, comprising an alkali metal magnesium orthosilicate and optionally either magnesium oxide or alkali metal silicate products is contacted with water to form a second composition comprising solid amorphous magnesium silicate hydrates (and optionally solid magnesium oxide or hydroxide), together with an aqueous solution comprising alkali metal cations, hydroxide anions and silicate anions.\|[0040] The first composition as, for example pellets or nodules, is preferably quenched in an amount of water, such that the final mixture after quenching has a temperature close to, but not exceeding, about 100° C., i.e. enough to quench the solids but avoiding excessive evaporation of water. The hot quenched solids are then preferably crushed and agitated mechanically in the form of a slurry. More water may be added if necessary. Some additional heating may be necessary.\|[0041] Alternatively the treatment with water, for example in the quenching and slurry-formation process described above, can be conducted at a temperature above 100° C. if a pressurized vessel (e.g. an autoclave) is used.\|[0042] Alternatively the above quenching and slurry-formation process can be conducted at lower or ambient temperatures. Water for converting the first composition into the second composition can optionally be recycled from another part of the process.\|[0043] The objective is to separate the components of the second composition by virtue of the facts that (a) alkali metal carbonates, silicates, chromates, sulfates and oxides or hydroxides in the product will tend to dissolve readily in water; (b) alkali metal magnesium orthosilicates will tend to hydrate in hot water to release alkali metals into solution as silicates and hydroxides, the remainder giving a fine suspension of solid amorphous magnesium silicate hydrates, and (c) magnesium oxide (MgO, also known as periclase) in the sample will tend to hydrate in hot water to give magnesium hydroxide (Mg(OH)2, also known as brucite) to form a soft and easily-dispersible powder.\|[0044] The slurry may need to be agitated mechanically. Then, the liquid phase can be separated from the bulk of the unreacted alkali metal magnesium orthosilicate and other unreacted anhydrous compounds, for example by sieving, and the fine particles of magnesium hydroxide and/or amorphous magnesium silicate hydrates which pass through the sieve as a slurry may be separated from the slurry by, for example, filtering, passage through a hydrocyclone, settling and/or centrifuging. The aqueous phase after separation of the magnesium hydroxide comprises an aqueous solution of alkali metal silicates and hydroxides.\|[0045] Alternatively, the separation process may be conducted in two steps, the first step comprising a rapid washing process to remove most of the readily soluble alkali metal carbonates, silicates and hydroxides; and the second step, conducted with additional water, comprising further hydration of both the magnesium oxide and the alkali metal magnesium orthosilicate. In this two-step approach, the water temperature is preferably lower for the first step (for example lower than 60° C.) than for the second step, and an autoclave may be used for the second step if necessary.\|[0046] The overall result of the separation process described above can be summarized as follows:\|[0047] Solid products from the process of the invention, e.g. from the furnace or kiln, (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4, MgO or R2SiO3, QO, and possibly some residual R2CO3) are contacted with water to produce a second composition comprising:\| - (a) a fine suspension comprising amorphous magnesium silicate hydrates and optionally Mg(OH)2 in a highly alkaline solution rich in alkali metal silicates, hydroxides and possibly also carbonates, and\| - (b) coarse unreacted solids comprising R2MgSiO4, and optionally MgO, QO and unreacted particles of the original magnesium silicate rock (e.g. Mg2SiO4), and which separate easily by sedimentation (e.g. in a hydrocyclone) from the fine suspension.\|[0050] The fine suspension can then be further separated (e.g. by filtration) to give\| - (c) fine solids rich in amorphous magnesium silicate hydrates and optionally Mg(OH)2, and\| - (d) a solution rich in alkali metal silicates, hydroxides and possibly also carbonates, and also comprising minor amounts of alkali-soluble impurities, e.g. sulfates and chromates.\|[0053] The initial part of the reaction of the solid products in the process of the invention with water can be written qualitatively as follows, for m≧1 (equation 2a), and m≧1 (equation 2b):\|(m−1)MgO+R2MgSiO4(m−1)Mg(OH)2+“M-S—H”+2R++(OH−,H2SiO4═,CO3═) (2a)\|(1−m)R2SiO3+mR2MgSiO4“M-S—H”+2R++(OH−,H2SiO═,CO3═) (2b)\|[0054] In the above reactions, the main solid compounds produced are an amorphous magnesium silicate hydrate, “M-S—H”, of variable composition, plus, in the case where m>1, magnesium hydroxide (brucite). The alkali metals may dissolve completely in the aqueous phase as alkali metal cations (R+), and the charge of these alkali metal cations is balanced by a mixture of dissolved anions, e.g.: hydroxide (OH−), silicate (H2SiO4═) and possibly also carbonate (CO3═), present in various ratios depending on the conditions and materials used. It is to be understood that equations 2(a) and 2(b) are not perfectly balanced equations but rather are simply intended to indicate the main initial products of the reaction between the solid products of the process of the invention with water.\|[0055] In a further embodiment of the invention the alkaline solution produced in step (d) is contacted with a carbon dioxide-containing gas, for example combustion exhaust gases, to absorb carbon dioxide and yield an alkali metal carbonate, alkali metal bicarbonate or a mixture thereof, generally in solution, and (precipitated) silica.\|[0056] For example, the aqueous solution from step (d) comprising mainly alkali metal hydroxides and silicates and also some residual alkali metal carbonates is contacted with a carbon dioxide-containing gas, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. The solution rapidly absorbs CO2 from such gases to produce a solution of alkali metal carbonates and bicarbonates, and a precipitate of amorphous silica, according to the following, or similar, equations:\|CO2(gas)+2ROH(in solution)R2CO3(in solution) (3)\|CO2(gas)+R2SiO3(in solution)R2CO3(in solution)+SiO2(solid precipitate) (4)\|CO2(gas)+R2CO3(in solution)2RHCO3(in solution) (5)\|[0057] The resulting solid silica precipitate is separated from the solution, for example by filtering, passage through a hydrocyclone, settling and/or centrifuging. In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled. Additional solutes, e.g. known salts, may also be incorporated into the solution. The precipitated silica formed by reaction (4) above can be separated, washed and dried for use in various applications.\|[0058] It will be understood by mass balance that reactions (3) and (4) should in principle be able to absorb essentially all of the CO2 released by the chemical reaction occurring in the process of the invention as shown in reaction (1), but that the additional CO2 resulting from the combustion process required to heat the starting materials will require an additional reaction to absorb it completely, e.g. either a reaction such as (5), or a further reaction with another absorbent.\|[0059] The present invention thus provides a process as described hereinbefore which further comprises isolating or producing magnesium oxide, magnesium hydroxide or an alkali metal silicate from the second composition.\|[0060] In a further embodiment of the invention, the second composition comprising M-S—H is carbonated, i.e. contacted with a carbon dioxide-containing gas, preferably in the presence of water, to produce a third composition comprising a magnesium carbonate compound. The rate of this reaction can be controlled by the temperature, the pressure, the relative humidity, the presence of catalysts and/or the type of reactor used. The carbonation reaction may be represented for example by the equation:\|sCO2(gas)+pMgO.SiO2.qH2Os“MgCO3”+(p−s)MgO.SiO2.q′H2O (6)\|[0061] The first product of this carbonation reaction, shown above as “MgCO3” may be either a simple magnesium carbonate, such as magnesite (MgCO3) or nesquehonite (MgCO3.3H2O), or a complex magnesium hydroxy-carbonate hydrate such as hydromagnesite (Mg(OH)2.4MgCO3.4H2O), or artinite (Mg(OH)2.MgCO3.3H2O), depending on the conditions employed. The second product of this reaction, shown above as “(p−s)MgO.SiO2.q′H2O” represents either an amorphous magnesium silicate hydrate with a lower magnesium/silicon ratio (p−s) than that (p) of the starting magnesium silicate hydrate; or, in the case where p=s, it represents simply a (hydrated) amorphous silica.\|[0062] In a further embodiment of the invention the coarse, partially reacted solids separated from the reaction products in step 1(b) above comprise mainly unreacted magnesium silicate (for example, Mg2SiO4) mixed with some intermediate products (for example, Na2MgSiO4). These can be dried and recycled to be mixed with additional raw magnesium silicate starting material for feeding back into the process. It will be understood that drying should be accomplished in an energy-efficient manner, e.g. first by drainage and then by use of waste heat from the furnace or other sources.\|[0063] According to a further feature of the invention all of the solid products from the process of the invention, e.g. from the furnace or kiln (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4 and MgO or R2SiO3 and/or QO, and possibly some residual R2CO3) are ground together with water to produce a suspension or slurry which is then contacted with a gas containing carbon dioxide, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. During this treatment, in addition to the other reactions described above, (e.g. in equations (2), (3), (4), (5) and (6)), the alkali metal magnesium orthosilicate compound can also react directly with CO2 as indicated by equations (7) and (8) below:\|R2MgSiO4+2CO2MgCO3(solid)+SiO2(solid)+R2CO3(in solution) (7)\|or, alternatively, making use of an alkali bicarbonate solution to achieve the same reaction:\|R2MgSiO4+4RHCO3MgCO3(solid)+SiO2(solid)+3R2CO3(in solution) (8)\|[0064] The alkali metal bicarbonate RHCO3 used in reaction (8) may be formed by the reaction of alkali metal carbonate solution R2CO3 produced in reaction (7) with carbon dioxide, as shown in equation (5).\|[0065] Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300° C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eitelite, Na2CO3.MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|[0066] These types of reaction are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid products. The magnesium carbonate solid produced can be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3.3H2O), or a complex magnesium hydroxy-carbonate hydrate, such as hydromagnesite (Mg(OH)2.4MgCO3.4H2O), or artinite (Mg(OH)2.MgCO3.3H2O), depending on the conditions and starting materials. The silica solid produced can be either a simple amorphous silica or a more complex mixed metal hydroxy-silicate such as an amorphous magnesium silicate hydrate (“M-S—H”). The alkali metal carbonate or bicarbonate solutions resulting from complete carbonation as shown in reactions (3), (4), (5), (7) and (8) can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and then recycled to the start of the process. The solid mixture of magnesium carbonates and silica produced by these reactions is one of the final products of the overall process and, after washing if necessary to recover as much as possible of the soluble alkali metal salts, can be separated for disposal or for use in other processes.\|[0067] The overall object of the process is to convert magnesium silicate rock into useful industrial products with low overall CO2 emissions. A further benefit of the process is to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable mineral carbonate which comprises a magnesium carbonate compound. Below are some examples of some different ways in which the process can be used:\|[0068] Starting with a magnesium silicate rock of composition m(MgO).t(QO).SiO2.xH2O, and recycling substantially all of the alkali metal (R) compounds used back into the process, at least two separate major product streams can be secured from amongst the following:\| - (i) Products rich in magnesium oxide or hydroxide (MgO or Mg(OH)2)\| - (ii) Products rich in amorphous silica (SiO2)\| - (iii) Products rich in amorphous magnesium silicate hydrates (M-S—H)\| - (iv) Products rich in magnesium carbonate compounds, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3, also known as magnesite); or magnesium carbonate trihydrate (MgCO3.3H2O, also known as nesquehonite); or magnesium hydroxy-carbonate hydrate, such as\|[0073] (Mg(OH)2.4MgCO3.4H2O), also known as hydromagnesite, or (Mg(OH)2.MgCO3.3H2O), also known as artinite.\|[0074] Improved separation of the above major solid product streams can also be achieved by the application of other known mineral separation techniques such as, for example, flotation. Such flotation techniques can be effected using flotation aids including sodium oleate, carboxymethylcellulose and methyl isobutyl carbinol.\|[0075] To the extent that CO2 is produced by the combustion of fuels used in the process, e.g. to heat the kiln or furnace, or to dry materials, this CO2 can be captured in the process in the form of product (iv) listed above, by using a treatment process based on the reactions shown above. To the extent that the process is energy-efficient, the aforesaid CO2 produced by the combustion of fuels used in the process, even if substantially completely captured by reactions of the sort shown, for example, in equations (3), (4) and (5), will generally not be sufficient to convert all of the magnesium in the process to product stream (iv), leaving some of the magnesium available for the production of product streams (i) and (iii). However, in another embodiment of the process, additional CO2 can be obtained from other sources and included in the treatment process and thus captured. In such a case, it is possible to operate the process in such a way that product stream (i) is not produced, but the process itself becomes a net consumer of CO2. Moreover, it is also possible to operate the process without separating any of the product streams, so that the only product stream produced is a mixture of some or all of the above product streams\|[0076] In a further approach, the process uses the same magnesium silicate raw material as shown above, but in this case, not all of the alkali metal-rich products of the process are recycled within the process. It is therefore possible to have one or more additional product streams as well as those already listed above. For example, one very useful product stream is an alkali metal silicate, (R2SiO3), either in the form of an alkaline aqueous solution also containing alkali metal hydroxides and/or carbonates, or as a solid product, (for example, obtained by evaporation and/or crystallization).\|[0077] According to a feature of the invention the process further comprises carbonation of the second composition, e.g. by treatment with gases containing CO2, to produce a third composition comprising a magnesium carbonate, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3), also known as magnesite; or magnesium carbonate trihydrate (MgCO3.3H2O), also known as nesquehonite; or magnesium hydroxy-carbonate hydrates, such as (Mg(OH)2.4MgCO3.4H2O), also known as hydromagnesite, or (Mg(OH)2.MgCO3.3H2O), also known as artinite.\|[0078] According to a further feature of the invention, the process further comprises conducting the carbonation of the second composition as described in the preceding paragraph, but where the second composition is first formed by moulding or pressing to form a shaped article, such that the resulting final carbonated composition retains the form of the shaped article but is further hardened by the formation of magnesium carbonates in situ. The present invention thus provides a process as described hereinbefore, in which the carbonation of the second composition is conducted in a second step, after a first step during which the second composition is formed by moulding or pressing to form a shaped article, such that a carbonated shaped article is obtained.\|[0079] The present invention further provides a carbonated shaped article obtained by the process as described hereinbefore.\|[0080] According to a further feature of the invention the process further comprises calcining the magnesium carbonate from the third composition to produce a fourth composition comprising magnesium oxide.\|[0081] The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|[0082] Another useful product stream is rich in transition metal oxides, for example iron oxides such as magnetite (Fe3O4), and which may also contain significant amounts of chromium and/or nickel oxides. These oxides can be concentrated by flotation and/or magnetic separation.\|[0083] Another useful product stream is an alkaline solution containing chromates, which can be treated with a reducing agent and pH control (or by electrochemical reduction) to separate relatively pure chromium oxides, or even chromium metal; for example:\|R2CrO4(aqueous solution)+(reducing agent)Cr(OH)3(solid precipitate)\|[0084] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0085] The term “pellets” as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0086] Particle size distribution when measured by laser granulometry is measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He—Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.\|[0087] The apparatus is checked before each working session by means of a standard sample (Sifraco 010 silica) for which the particle size distribution is known.\|[0088] Measurements are performed with the following parameters: pump speed 2300 rpm and stirrer speed 800 rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30 s (for possible air bubbles to clear), a measurement is carried out for 15 s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0089] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0090] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R, Q, m, t, x and, p are as initially defined.\|[0091] The following non-limiting Examples illustrate embodiments of the invention.\|[0092] The following abbreviations and notations are used:\| - XRF X-ray fluorescence\| - XRD X-ray diffraction\| - ICP Inductively-Coupled Plasma Photometry\| - Hydromagnesite Mg(OH)2.4MgCO3.4H2O\| - Artinite Mg(OH)2.MgCO3.3H2O\| - Eitelite Na2CO3.Mg(CO3)\| - LOI Loss on ignition\|(US9631257)\|EXAMPLE 1\|[0100] Ground pure olivine sand (Mg0.94Fe0.06)2SiO4 was mixed with sodium carbonate hydrate powder in a 14:11 mass ratio. The molar ratio of this mixture is close to 1:1. 25 g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800° C. over 2 hours, maintained at 800° C. for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table.\|[0101] SampleLoss on Ignition Sodium carbonate powder14.97% Ground olivine sand0.22% 14:11 mix of ground olivine sand +16.69% sodium carbonate powder \|[0102] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by XRD. The reaction products observed by this technique were Na2MgSiO4, MgO and Fe2O3 together with some unreacted olivine and sodium carbonate.\|[0103] 10 g of the reacted sample was put into 100 ml of de-ionised water under constant stirring at 40° C. for 1 h in order to evaluate its dissolution behaviour. The solution was filtered and the solid residue was analysed by XRD. The amounts of dissolved elements in the aqueous solutions were measured by ICP.\|[0104] The main solid phases detected in the filtered solid residue were Na2MgSiO4, MgO, Fe2O3 and olivine. All non-reacted sodium carbonate dissolved in the aqueous solution. Additionally, some dissolved SiO2 was detected with a concentration of 667 mg/I. From this value, one can estimate that 2 to 3% of the total silica from the mixture dissolved in the water under these conditions, (presumed to be as a sodium silicate, as the pH of the solution was measured to be about 12).\|EXAMPLE 2\|[0105] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. The molar ratio of this mixture is approximately 1:1. The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900° C. The sample was air-quenched after 1 h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851° C.). The measured loss on ignition of all of the samples is presented in the following Table.\|[0106] SampleLoss on Ignition Sodium carbonate14.96% Olivine0.04% Olivine + Sodium carbonate23.02% \|[0107] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by XRD and the phases detected were Na2MgSiO4, MgO, NaFeO2 together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data. The MgO to Na2MgSiO4 mass ratio was estimated by Rietveld analysis of the XRD data to be 14:86, in reasonable agreement with mass balance calculations.\|EXAMPLE 3\|[0108] 13 g of the powdered product of Example 2 was mixed with 260 ml of water to give a slurry with about 50 g/L solids concentration. This slurry was put in a closed pressure reactor with a total volume of 2 liters, maintained at 25° C. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas and the pH of the aqueous solution were recorded as functions of time and are presented in FIG. 2. The rate of pressure drop indicates that the slurry captures gaseous CO2 rapidly, and, concurrently, the pH of the solution falls rapidly from an initial value of over 12 to a final value of about 8.5, consistent with the formation of a mixed sodium carbonate/bicarbonate solution. After this reaction the solids in the slurry were filtered and analysed by XRD. NaFeO2 was no longer detectable and the MgO:Na2MgSiO4 ratio had increased to an estimated value of 18:82, indicating that some sodium silicate had leached out of the Na2MgSiO4 phase into the solution and had then been carbonated.\|EXAMPLE 4\|[0109] 5 g of the powdered product of Example 2 was mixed with 200 ml of water to give a slurry of about 25 g/L solids concentration. This slurry was then boiled gently for one hour, after which it was filtered and the solid residue analyzed by XRD. The relative concentration of the Na2MgSiO4 phase in the residue was clearly greatly reduced compared to the original untreated residue, and the relative concentration of MgO greatly increased. The NaFeO2 phase had also completely disappeared but peaks for a layered double hydroxide phase probably having a formula close to 4MgO.Fe2O3.CO2.10H2O were seen clearly, together with weaker peaks for Fe2O3 (haematite) and unreacted olivine.\|[0110] The liquid filtrate was also analyzed by ICP and the results (see the Table below) showed a high concentration (6.92 g/L as Na2O) of sodium in solution, as well as 0.47 g/L of SiO2. This confirms that most of the sodium had leached out of the sample, and that about 15% of it was probably in the form of a sodium metasilicate solution, the rest presumed to be a mixture of sodium hydroxide and sodium carbonate.\|[0111] Chemical analysis of the aqueous solution Chemical speciesConcentration [mg/l] SiO2466 Al2O36.65 Fe2O31.78 CaO0.51 MgO1.51 K2O2.40 Na2O6920 SO32.53 P0.58 \|EXAMPLE 5\|[0112] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 liters, maintained at 35° C. and agitated with a mechanical stirrer operating at 500 rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its absorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in the following Table.\|[0113] CO2 Total captured, CO2Slurry SlurryTotalas % of Experimentcapturedvolumeconc.solids. theoreticalSlurryTemp.DurationSolid productsn° (mol)(mL)(g/L)(g)maximumadditives(° C.)(h)detected 10.06412605013.035Na2CO3:3524Hydromagne 21.15 g/L site20.07242605013.040Na2CO3:3524Hydromagne 53.85 g/L site30.13632605013.075NaHCO3:3530Hydromagne 53.85 g/L site40.035226011.52.9984 3526Artinite \|[0114] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite and, in one case, artinite, which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 6\|[0115] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometer sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950° C.), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio (molar ratio approximately 1:1.3). About 5 kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950° C. for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by XRF spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3, and 33.4% sodium expressed as Na2O. An XRD analysis showed the major phases present in the product to be Na2MgSiO4 and periclase (MgO).\|EXAMPLE 7\|[0116] The reaction products of Example 2 (referred to hereinafter as “product X”) and of Example 6 (referred to hereinafter as “product XS”) were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75 g of the solid were added to 1.5 liters of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500 rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal liters per hour at close to one atmosphere absolute pressure. The reactor contents were maintained at 70° C. by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements by ICP. The solid filter-cakes were dried at 110° C. and then analysed by XRF spectrometry for elemental composition, by XRD for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0117] The results for three different product samples are given in the following Table\|[0118] Blaine EstimatedMg inEstimated specificMainTotal Mg Mg inaqueousdegree of surfacecrystallinecontent ofCO2hydro-phasereaction ofExperiment area ofphasesdried filter-contentmagnesiteexpressedMgO inN°; anhydrousdetected incake,of driedexpressedas % MgOanhydrousanhydrousDurationproduct,dried filter- expressedfilter-as % MgOrelative toproduct,product used(h)m2/kgcakeas MgO, %cake, %in filter-cakefilter-cake% 53.5420Hydro-31.215.918.20.659Product X magnesite 614.0600Hydro-30.316.418.80.563Product X magnesite 74.0205Hydro-27.717.219.70.471Product magnesite XS 1In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0119] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields of the order of 60-70% of the total magnesium in the starting material in about 3.5 to 4 hours. Based on XRF analyses of the solid phases coupled with ICP analyses of the liquid phase, it is estimated that roughly 90% of the initial Na and 50% of the initial Cr in the product leached out during the experiment.\|EXAMPLE 8\|Formation of Eitelite\|[0120] The procedure of Example 7 was repeated using two slurries (prepared from products X and XS from Examples 2 and 6, respectively) at a concentration of 150 g/L, i.e. three times the concentration used in Example 7.\|[0121] During the 3 first hours the same trends were observed as those in Example 7. But after 4 hours, XRD revealed the presence of eitelite as well as hydromagnesite. The results are given in the following Table.\|[0122] Blaine Mg inEstimated specificMainTotal Mg Estimatedaqueousdegree of surface areacrystallinecontent ofCO2Mg in hydro-phasereaction ofExperiment ofphasesdried filter-contentmagnesiteexpressedMgO inN°; anhydrousdetectedcake,of driedexpressedas % MgOanhydrousanhydrousDurationproduct,in driedexpressedfilter-as % MgO inrelative toproduct,product used(h)m2/kgfilter-cake as MgO, %cake, %filter-cakefilter-cake% 84.0600Hydro-28.0616.4518.830.567.12Product X magnesite & eitelite 94.0600Hydro-25.7415.8218.110.870.37Product magnesite XS & eitelite \|EXAMPLE 9\|Effectiveness of Water Leaching\|[0123] 50 g of product X was washed in 1 L deionised water 6 times in series (15 minutes stirring in between at room temperature and atmospheric pressure, i.e. 25° C. and 1 bar). Each time a small sample was taken to analyse the solids and the liquids. The XRF results for product X coupled with ICP solution analyses lead to the results given in the following Table, which the percentages of each element leached from the product are given as a function of the number of washing steps.\|[0124] % leachedSiCaMgKNaSCr Washing 19.850.460.0019.7636.4413.7746.12Washing 23.200.090.00 1.94 8.69 0.60 1.30Washing 31.410.020.00 0.25 3.47 0.04 0.21Washing 41.220.020.00 0.03 3.53 0.13 0.32Washing 50.750.020.00 0.02 1.87 0.14 0.12Washing 60.510.050.00 0.00 1.30 0.05 0.08TOTAL16.940.660.0122.0055.3114.7348.15 \|[0125] The first washing step was clearly the most efficient. Therefore 500 g of product X were washed in the same conditions, the solid was then filtered and dried overnight at 110° C. Finally the same carbonation experiment as described in Example 8 was performed on this solid product. This time XRD analysis revealed only hydromagnesite; no eitelite was detected. This shows that washing can be used to enhance Na recycling in the process.\|[0126] The analysis of the solution obtained after the first washing (table below) showed it to have a high pH and to contain about 4000 mg/L of Na and 637 mg/L of Si, the other elements being present in much smaller amounts. On this basis, the solution was estimated to contain about 23 milimoles/liter of sodium metasilicate (Na2SiO3) and 130 millimoles/liter of sodium hydroxide (NaOH), possibly also including some carbonate ions.\|[0127] In mg/l (elements)SiCaMgKNaSCr Washing 1637.50.2990.2674.140001.3828.4 \|EXAMPLE 10\|Hydromagnesite Formation at 60° C.\|[0128] 1 L of a 50 g/L slurry of product X was prepared and poured into a 2 L autoclave. The system was closed and 1 L of pure CO2 at 10 bars was added without purging the residual air, after which the slurry was stirred and heated up to 60° C. (which roughly corresponds to the dew point of exhaust gases in a cement plant). After 2 hours the pressure dropped to close to atmospheric and heating of the autoclave was stopped. The next day, the slurry was filtered and dried overnight at 110° C. XRD revealed hydromagnesite as the main crystalline product.\|EXAMPLE 11\|Formation of Magnesite as Main Product at 120° C.\|[0129] The procedure of Example 10 was repeated but at 120° C. (a typical temperature for exhaust gases from a cement plant) using the same autoclave, and adding CO2 each time the pressure dropped close to two bars (the equilibrium water vapour pressure at 120° C.). Three additions of CO2 up to 10 bars were made in the space of one day. XRD on the dried solid revealed magnesite (MgCO3) to be the main product, but also showed some traces of magnetite (Fe3O4). ICP analysis of the aqueous phase showed 90% leaching of Na. The combined CO2 content in the solids was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser and showed that the amount of MgCO3 present accounted for about 47% of the original Mg in Product X.\|EXAMPLE 12\|Selective Separation of Chromium by Reduction in Solution\|[0130] Powdered product X was stirred with deionised water for 15 minutes at a 2:1 Water:solids mass ratio. The yellow-coloured aqueous phase was filtered and a sample taken for ICP analysis. Excess ferrous sulfate (FeSO4), a reducing agent, was then added in powder form to the solution, after which a chromium-containing precipitate formed. The liquid was again filtered, giving a colourless solution which was again analysed by ICP. The chromium content of the yellow-coloured aqueous phase was 772 mg/L. The colourless solution contained only 29 mg/L of chromium.\|[0131] These results, when compared with the analysis of the raw materials, indicated that about 50% of the total chromium in the original raw material (olivine) was converted into a readily soluble (chromate) form by the process used to make “product X,” and 96% of the Cr leached into the solution was precipitated by addition of ferrous sulfate.\|EXAMPLE 13\|Concentration of Hydromagnesite from the Solid Residues by Flotation\|[0132] Separation tests were performed by flotation on the carbonated products produced from the application of the process to olivine and serpentine, similarly to the products shown, respectively, for experiments 5 and 7 in the table of Example 7. Combinations of sodium oleate, carboxymethylcellulose (CMC) and methyl isobutyl carbinol (MIBC) were used in the aqueous phase sequentially to disperse the solids in the form of a slurry at a solids concentration of 90 g/L.\|[0133] First sodium oleate was added to the slurry and stirred for 5 minutes in a beaker in order to render carbonated particles hydrophobic. Then CMC was added to depress silicate hydrophobicity, followed by a further 5 minutes of stirring; and finally MIBC was added in order to stabilise the foam formed by air bubbling.\|[0134] Air was bubbled through the treated slurry in a miniature flotation cell, and the solids carried over by the foam were collected as “concentrate.” The residual solids were collected as “tailings.” Results of four such experiments are presented in the table below. The CO2 content was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser. The CO2 contents of the concentrates were typically 3-4 times greater than those of the tailings, showing that hydromagnesite can be effectively separated by flotation in this manner.\|[0135] The XRD results confirm the separation. They are expressed in a qualitative way by different symbols expressing the probability of a phase presence:\| - (o) not present,\| - () possibly present,\| - (X) definitely present,\| - (X+) present in abundance.\|[0140] Chemical additive (dosage, ppm)Test 1Test 2Test 3Test 4 Sodium oleate1500100020001000CMC200200200200MIBC20202020Product tested by flotation:Carbonated “product X”Carbonated “product X”Carbonated “product X”Carbonated “product XS”Results of flotation testsTailingsConcentrateTailingsConcentrateTailingsConcentrateTailingsConcentrateComponents SiO2 %34.117.633.718.533.822.033.316.9measured byFe2O3 %6.43.46.43.66.44.36.93.0chemical MgO %34.637.234.537.233.936.929.235.9analysisNa2O %2.31.32.31.42.61.32.31.2 LOI %22.340.022.638.922.735.126.241.6 CO2 %5.722.25.820.25.717.39.423.0Phases Sodium 00000000detected bymagnesium XRDsilicate PericlaseXXX** OlivineXXX*00 HydromagnesiteXX +XX +XX +XX + \|EXAMPLE 14\|[0141] Ground natural talc from Luzenac (France) with nominal composition Mg3Si4O10(OH)2 and containing some minor impurities (1.1% Al2O3, 0.9% Fe2O3 and 0.9% CaO by mass) was mixed with anhydrous sodium carbonate (Na2CO3) at a 4863:5136 mass ratio (molar ratio approximately 1:1). The composition was chosen in order to obtain an atomic ratio of 2:1 Na:Si in the final sample. 20.5 g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. The sample was heated at 900° C. for 1 hour, followed by cooling in air. It was weighed before and after treatment and the measured loss on ignition of 23.3% was consistent with evaporation of carbon dioxide from the sodium carbonate plus bound water from the talc; it represents about 95% of the theoretical value for complete reaction of 24.6%. The phase constitution of the reacted sample was determined by X-ray diffraction: the main products detected were Na2MgSiO4 and Na2SiO3.\|EXAMPLE 15\|[0142] A sample of Product X was leached in water following a procedure similar to that given in example 9. After drying at 105° C., the powdered material (which had an ignition loss of 8.9%), was analyzed by X-ray fluorescence for its major elements, and found to contain 28.1% SiO2, 39.1% MgO and 17.9% Na2O. An X-ray diffraction analysis showed that the main crystalline compounds present in the powder were periclase (MgO), sodium magnesium orthosilicate (Na2MgSiO4) and forsterite olivine (Mg2SiO4); but it was known also to contain amorphous magnesium silicate hydrates (M-S—H). 5 parts of this material were mixed manually with 1 part of deionised water in a rubber bowl, using spatula. 7 g aliquots of the resulting paste were compressed in a cylindrical mould at a load of 3 tonnes to give cylindrical pellets 19 mm in diameter and 10 mm in height. These pellets were subject to curing in a flow of pure CO2 gas at atmospheric pressure in a chamber at 20±2° C. Two different humidity conditions were tested: dry (i.e. no water added to the gas stream); and wet (in which the gas stream was bubbled through water at the bottom of the curing chamber before passing over the pellets). The uptake of CO2 and/or water by the pellets was followed by taking them out quickly and weighing them once a day. The experiment was stopped after one week, as the weight increases had begun to level off. At this point, the pellets carbonated under dry conditions had gained 3.0% and all four of the pellets tested gave essentially identical weight changes. On the other hand, the pellets carbonated under wet conditions (close to 100% relative humidity) showed a wider pellet-to pellet variation in weight increase, with a mean of 7.8% and a standard deviation of about 1%.\|[0143] It was notable that all of the pellets that had been carbonated under one atmosphere of CO2 became superficially much harder than companion pellets that had simply been stored in air. The pellets carbonated under humid conditions also showed a considerable amount of efflorescence. A sample of this efflorescence was scraped off and analyzed by X-ray diffraction. It was found to contain nesquehonite (MgCO3.3H2O), nahcolite (NaHCO3), trona (Na3H(CO3)2.2H2O), and sodium carbonate mono-hydrate (Na2CO3.H2O). The wet-carbonated pellets themselves, analyzed by the same technique, showed the presence of primarily of periclase (MgO), sodium magnesium orthosilicate (Na2MgSiO4), olivine (Mg2SiO4) and nesquehonite (MgCO3.3H2O). It thus appears that nesquehonite was the main “binder” phase and that it was probably produced to a significant extent by carbonation of M-S—H.\|[0144] Pairs of treated and untreated pellets were compressed to failure in a compression machine. The results are summarized in the table below:\|[0145] Compressive loads at failure,Curing regime applied to pressed pelletskN, (for 2 pellets) Stored in air3.0; 3.2Carbonated under humid conditions11.5; 18.5Carbonated under dry conditions36.0; 36.7 \|[0146] It is clear that the atmospheric-pressure carbonation process greatly increased the strength of the pellets, and that carbonation under dry conditions was preferable to carbonation under humid conditions.	Family Number\|(66131709)\|66131709\|Advantages / Prev. Drawbacks\|(WO201482996 A1)\|According to one manufacturer of such products hectorites have the formula (Mg5.2Lio.8)(Si8)02o(OH)4Nao.8- The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (C02) and which can be subjected to further treatments to produce a number of useful products.\|(CA2892325 A1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO 2 ) and which can be subjected to further treatments to produce a number of useful products.\|(AU2013351282 B2)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|(AU2013351282 A1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|(CN104812468B B)\|The present invention seeks to provide a process for producing alkali metal magnesium orthosilicates and magnesium oxide and / or alkali metal silicates from magnesium silicate rocks and which can be used to undergo chemical action to capture carbon dioxide ( CO ) 2 ) And may be subjected to further processing to produce a variety of useful products . \|(CN104812468 A)\|The present invention seeks to provide a process for producing alkali metal magnesium orthosilicates and magnesium oxide and / or alkali metal silicates from magnesium silicate rocks and which can be used to undergo chemical action to capture carbon dioxide ( CO ) 2 ) And may be subjected to further processing to produce a variety of useful products . \|(KR20150088845 A)\|The present invention relates to carbon dioxide (Co2alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicate from magnesium silicate rock, which can be used in chemical treatments that capture a number of useful products and can be subjected to further treatments to produce a number of useful products.\|(US9631257 B2)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|(US20150299823 A1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|	Chemical engineering\|Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-2251/402\|B01D-2253/106\|B01D-2257/504\|B01J-020/10\|B01J-020/30/85\|C01B-033/22\|C01B-033/24\|C01B-033/32\|C01F-005/06\|C01F-005/24\|C04B-028/10\|C04B-028/18\|C04B-028/18/4\|C04B-2111/00019\|C22B-001/00\|C22B-026/22\|Y02C-010/04\|Y02C-020/40\|Y02P-010/146\|Y02P-020/151\|Y02P-020/152\|Y02P-040/18	(GR1) C04B-028/18/4[RK1]; 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Лидин Р.А., Москва, Дрофа, 2007, с. 285.	US3954943; WO2009132692; WO200769902; WO201097451; XP002994928; US20040213705; EP2532624\|US3954943; RU2011111500; WO2009132692\|US3954943; WO2009132692; EP2532624; US4478796; US20080112868; US20100151243; US20120291675; US2008112868; US2010151243; US2012291675\|US4478796; US20080112868; CN101607721\|US4478796; US20080112868; US20100151243; US3954943; US5085838; US6054106; US20040213705; US20120291675; EP2508496; EP2532624; WO200769902; WO2009132692; WO2009156740; WO201097451; XP002994928\|JP11512376; US3954943; JP2009084132\|US3954943; WO2009132692; WO200769902; WO201097451; US20040213705; EP2532624; US-837672; US20120291675\|\|\|	(EP2925426)\|Examiner references\|-See also references of WO 2014082996A1\|\|(US9631257)\|Applicant references\|-International Search Report as issued in International Patent Application No. PCT/EP2013/074732, dated Mar. 11, 2014.\|-O'CONNOR W K, ET AL.: "Carbon dioxide sequestration by direct mineral carbonation: process mineralogy of feed and products.", MINERALS AND METALLURGICAL PROCESSING., SOCIETY FOR MINING, METALLURGY AND EXPLORATION, US, vol. 19, no. 2, 1 May 2002 (2002-05-01), US, pages 95 - 101, XP002994928, ISSN: 0747-9182\|\|(WO2014/082996)\|International Search Report [Examiner]\|-O'CONNOR W K ET AL: "Carbon dioxide sequestration by direct mineral carbonation: process mineralogy of feed and products", MINERALS AND METALLURGICAL PROCESSING, CO, vol. 19, no. 2, 1 May 2002 (2002-05-01), pages 95 - 101, XP002994928, ISSN: 0747-9182\|-See also references of EP 2925426A1\|\|\|\|\|\|\|\|	PENDING	(EP2925426)\|LAPSED\|(US9631257)\|LAPSED\|(WO2014/082996)\|LAPSED\|(JP2015536897)\|REVOKED\|(CN104812468)\|LAPSED\|(RU2654983)\|LAPSED\|(AU2013351282)\|EXPIRED\|(MX2015006607)\|PENDING\|(KR10-2015-0088845)\|LAPSED\|(CA2892325)\|LAPSED	ALIVE	(EP2925426)\|DEAD\|(US9631257)\|DEAD\|(WO2014/082996)\|DEAD\|(JP2015536897)\|DEAD\|(CN104812468)\|DEAD\|(RU2654983)\|DEAD\|(AU2013351282)\|DEAD\|(MX2015006607)\|ALIVE\|(KR10-2015-0088845)\|DEAD\|(CA2892325)\|DEAD	(EP2925426)\|LEGAL DETAILS FOR EP2925426\|Actual or expected expiration date=2018-04-10\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP13795508\|Application date=2013-11-26\|Standardized application number=2013EP-0795508\|Event publication date=2015-09-04\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2015-10-07\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2925426\|Publication stage code=A1\|Publication date=2015-10-07\|Standardized publication number=EP2925426\|Event publication date=2015-10-07\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2015-06-29\|Event publication date=2015-10-07\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2015-10-07\|Event code=EP/AX\|Event indicator=Pos\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT\|Request for extension of the european patent to\|Designated contracting states=BA ME\|Event publication date=2015-12-09\|Event code=EP/RAP1\|Event group=Change of name or address Reassignment\|Rights of an application transferred\|Anmelder uebertragung (korr.)\|OWNER:LAFARGE\|Event publication date=2016-03-02\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2016-06-15\|Event code=EP/17Q\|Event indicator=Pos\|Event group=Examination events\|First examination report\|Erster pruefungsbescheid\|Effective date of the event=2016-05-13\|Event publication date=2018-08-10\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2018-09-12\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2018-04-10\|(US9631257)\|LEGAL DETAILS FOR US9631257\|Actual or expected expiration date=2021-05-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US14647277\|Application date=2013-11-26\|Standardized application number=2013US-14647277\|Event publication date=2013-11-26\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:SOLIMAN, HAYTHAM\|Event publication date=2013-11-26\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2013-11-26\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 035112-0439264\|Event publication date=2013-11-26\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 909\|Event publication date=2013-11-26\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2013-11-26\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2015-05-26\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2015-05-26\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2015-05-26\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2015-05-26\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2015-06-08\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:PISCH, ALEXANDER;GARTNER, ELLIS;MEYER, VINCENT;SIGNING DATES FROM 20150518 TO 20150526\|Reel/frame:035803/0664\|OWNER:LAFARGE, FRANCE\|Event publication date=2015-07-13\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2015-07-13\|Event code=US/M903\|Event indicator=Pos\|Event group=Examination events OAO\|Notice of DO/EO Acceptance Mailed\|Event publication date=2015-08-20\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2015-09-18\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2015-09-23\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2015-09-23\|R4R=102b\|RJST=non-final\|Rejected claims 10\|RJCT=US20100151243\|Event publication date=2015-09-23\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2015-09-23\|R4R=103a\|RJST=non-final\|Rejected claims 1-6; 7\|RJCT=US4478796\|RJCT=US20080112868\|Event publication date=2015-09-24\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2015-09-24\|R4R=102b\|RJST=non-final\|Rejected claims 10\|RJCT=US20100151243\|Event publication date=2015-09-24\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2015-09-24\|R4R=103a\|RJST=non-final\|Rejected claims 1-6; 7\|RJCT=US4478796\|RJCT=US20080112868\|Event publication date=2015-10-22\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20150299823\|Publication stage code=A1\|Publication date=2015-10-22\|Standardized publication number=US20150299823\|Event publication date=2015-10-22\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2015-12-28\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2016-04-18\|Event code=US/CTFR\|Event group=Examination events OA OAO\|Final Rejection\|Event publication date=2016-04-21\|Event code=US/102FR\|Event indicator=Neg\|Event group=Examination events\|Final rejection reason 102 - non-novel subject matter in claims\|RJD=2016-04-21\|R4R=102b\|RJST=final\|Rejected claims 10\|RJCT=US20100151243\|Event publication date=2016-04-21\|Event code=US/103FR\|Event indicator=Neg\|Event group=Examination events\|Final rejection reason 103 - obvious subject matter in claims\|RJD=2016-04-21\|R4R=103a\|RJST=final\|Rejected claims 1-6; 7\|RJCT=US4478796\|RJCT=US20080112868\|Event publication date=2016-04-22\|Event code=US/102FR\|Event indicator=Neg\|Event group=Examination events\|Final rejection reason 102 - non-novel subject matter in claims\|RJD=2016-04-22\|R4R=102b\|RJST=final\|Rejected claims 10\|RJCT=US20100151243\|Event publication date=2016-04-22\|Event code=US/103FR\|Event indicator=Neg\|Event group=Examination events\|Final rejection reason 103 - obvious subject matter in claims\|RJD=2016-04-22\|R4R=103a\|RJST=final\|Rejected claims 1-6; 7\|RJCT=US4478796\|RJCT=US20080112868\|Event publication date=2016-07-19\|Event code=US/CTFAR\|Event group=Examination events OAI\|Response after Final Action\|Event publication date=2016-08-23\|Event code=US/EXET\|Event group=Examination events OAO INT\|Interview Summary - Examiner Initiated - telephonic\|Event publication date=2016-08-23\|Event code=US/CTAV\|Event group=OAO\|Advisory Action (PTOL-303)\|Event publication date=2016-10-21\|Event code=US/RCEX\|Event group=Examination events RCE OAI\|Request for Continued Examination (RCE)\|Event publication date=2016-10-21\|Event code=US/136G\|Event group=OAO\|Request for Extension of Time - Granted\|Event publication date=2016-10-21\|Event code=US/RCEX\|Event group=Examination events RCE OAI\|Request for Continued Examination (RCE)\|Action Recorded:\|RECD=2016-10-21\|Event publication date=2016-10-24\|Event code=US/DRCECAP\|Event group=RCE OAO\|Disposal for a RCE / CPA / R129\|Event publication date=2016-12-19\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2016-12-22\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2017-03-20\|Event code=US/NOARR\|Event group=Examination events\|Response to Reasons for Allowance\|Event publication date=2017-03-20\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2017-03-20\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2017-03-21\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2017-04-05\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2017-04-25\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US09631257\|Publication stage code=B2\|Publication date=2017-04-25\|Standardized publication number=US9631257\|Event publication date=2017-04-25\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 95 Adjustment total: \|Number of days of extension=0\|Event publication date=2019-01-18\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignor:LAFARGE\|Reel/frame:048061/0707\|OWNER:HOLCIM TECHNOLOGY LTD, SWITZERLAND\|Effective date of the event=2018-12-10\|Event publication date=2020-05-05\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2020-12-14\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2021-04-25\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2021-04-25\|Event publication date=2021-05-31\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2021-05-31\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|Event publication date=2024-05-07\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|(WO2014/082996)\|LEGAL DETAILS FOR WO2014/082996\|Actual or expected expiration date=2016-05-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOEP2013/074732\|Application date=2013-11-26\|Standardized application number=2013WO-EP74732\|Event publication date=2014-06-05\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2014/082996\|Publication stage code=A1\|Publication date=2014-06-05\|Standardized publication number=WO201482996\|Event publication date=2016-05-27\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2013351282\|Actual or expected expiration date=2020-06-25\|Legal state=DEAD\|Status=EXPIRED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2013351282\|Application date in the designated or member state=2013-11-26\|Application number in the designated or member state=2013AU-0351282\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2013351282\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2015-06-18\|Publication number in the designated or member state=AU2013351282\|Event publication 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state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2015-05-27\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2015-05-27\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP2925426\|Actual or expected expiration date=2018-04-10\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP13795508\|Application date in the designated or member state=2013-11-26\|Application number in the designated or member state=2013EP-0795508\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2925426\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2015-10-07\|Publication number in the designated or member state=EP2925426\|Event publication date=2014-07-23\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2015-05-13\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2018-09-12\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR JP2015536897\|Actual or expected expiration date=2018-08-22\|Legal state=DEAD\|Status=REVOKED\|Corresponding cc:\|Designated or member state=JP Corresponding appl: JP2015543468\|Application date in the designated or member state=2013-11-26\|Application number in the designated or member state=2015JP-0543468\|Corresponding cc:\|Designated or member state=JP Corresponding pat: JP2015536897\|Publication stage code in the designated 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in the designated or member state=MX2015006607\|Event publication date=2015-05-26\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=MX\|MEMBER STATE LEGAL DETAILS FOR RU2015125492\|Actual or expected expiration date=2019-11-27\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RU Corresponding appl: RU2015125492\|Application date in the designated or member state=2013-11-26\|Application number in the designated or member state=2015RU-0125492\|Corresponding cc:\|Designated or member state=RU Corresponding pat: RU2015125492\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2017-01-11\|Publication number in the designated or member state=RU2015125492\|Event publication date=2015-06-29\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national 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cc:\|Designated or member state=US\|Event publication date=2024-05-07\|Event code=US/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=US\|(JP2015536897)\|LEGAL DETAILS FOR JP2015536897\|Actual or expected expiration date=2018-08-22\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2013-11-26\|Event code=JP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=JP JP2015543468\|Application date=2013-11-26\|Standardized application number=2015JP-0543468\|Event publication date=2015-09-07\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2015-07-23\|Event publication date=2015-12-24\|Event code=JP/A\|Event group=Examination events\|Published application\|Publication country=JP\|Publication number=JP2015536897\|Publication stage code=A\|Publication date=2015-12-24\|Standardized publication 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the Patent Act, Expected Rejection Date\|Effective date of the event=2018-08-22\|(CN104812468)\|LEGAL DETAILS FOR CN104812468\|Actual or expected expiration date=2019-11-26\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201380061823\|Application date=2013-11-26\|Standardized application number=2013CN-80061823\|Event publication date=2015-07-29\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN104812468\|Publication stage code=A\|Publication date=2015-07-29\|Standardized publication number=CN104812468\|Event publication date=2015-07-29\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2015-11-11\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2017-08-25\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN104812468\|Publication stage code=B\|Publication date=2017-08-25\|Standardized publication number=CN104812468B\|Event publication date=2017-08-25\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2020-11-06\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee\|Effective date of the event=2019-11-26\|(RU2654983)\|LEGAL DETAILS FOR RU2654983\|Actual or expected expiration date=2019-11-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=RU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=RU RU2015125492\|Application date=2013-11-26\|Standardized application number=2015RU-0125492\|Event publication date=2017-01-11\|Event code=RU/A\|Event group=Examination events\|Application for invention\|Publication country=RU\|Publication number=RU2015125492\|Publication stage code=A\|Publication date=2017-01-11\|Standardized publication number=RU2015125492\|Event publication date=2018-05-23\|Event code=RU/C2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent for invention ( 2nd publ.)\|Publication country=RU\|Publication number=RU2654983\|Publication stage code=C2\|Publication date=2018-05-23\|Standardized publication number=RU2654983\|Event publication date=2019-03-01\|Event code=RU/PC41\|Event group=Change of name or address Reassignment\|Official registration of the transfer of exclusive right\|Effective date of the event=2019-03-01\|Event publication date=2019-04-29\|Event code=RU/PC41\|Event group=Change of name or address Reassignment\|Official registration of the transfer of exclusive right\|Effective date of the event=2019-04-29\|Event publication date=2020-09-21\|Event code=RU/MM4A\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The patent is invalid due to non-payment of fees\|Effective date of the event=2019-11-27\|(AU2013351282)\|LEGAL DETAILS FOR AU2013351282\|Actual or expected expiration date=2020-06-25\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=2013-11-26\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2013351282\|Application date=2013-11-26\|Standardized application number=2013AU-0351282\|Event publication date=2015-06-18\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2013351282\|Publication stage code=A1\|Publication date=2015-06-18\|Standardized publication number=AU2013351282\|Event publication date=2018-03-01\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent proceeded by OPI\|Publication country=AU\|Publication number=AU2013351282\|Publication stage code=B2\|Publication date=2018-03-01\|Standardized publication number=AU2013351282\|Event publication date=2018-06-28\|Event code=AU/FGA\|Event indicator=Pos\|Event group=Event indicating In Force\|Letters patent sealed or granted (standard patent)\|Event publication date=2019-02-21\|Event code=AU/PC\|Event group=Change of name or address Reassignment\|Assignment registered\|FORMER OWNER(S): LAFARGE\|OWNER:HOLCIM TECHNOLOGY LTD\|Event publication date=2020-06-25\|Event code=AU/MK14\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent ceased section 143(a) (annual fees not paid) or expired\|(MX2015006607)\|LEGAL DETAILS FOR MX2015006607\|Actual or expected expiration date=2033-11-26\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2013-11-26\|Event code=MX/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MX MX2015006607\|Application date=2013-11-26\|Standardized application number=2015MX-0006607\|Event publication date=2015-08-05\|Event code=MX/A\|Event group=Examination events\|Patent application\|Publication country=MX\|Publication number=MX2015006607\|Publication stage code=A\|Publication date=2015-08-05\|Standardized publication number=MX2015006607\|(KR10-2015-0088845)\|LEGAL DETAILS FOR KR10-2015-0088845\|Actual or expected expiration date=2018-12-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=KR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=KR KR10-2015-7016739\|Application date=2013-11-26\|Standardized application number=2015KR-7016739\|Event publication date=2015-08-03\|Event code=KR/A\|Event group=Examination events\|Published application\|Publication country=KR\|Publication number=KR10-2015-0088845\|Publication stage code=A\|Publication date=2015-08-03\|Standardized publication number=KR20150088845\|Event publication date=2018-12-27\|Event code=KR/WITN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Withdrawal due to no request for examination\|(CA2892325)\|LEGAL DETAILS FOR CA2892325\|Actual or expected expiration date=2020-08-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2892325\|Application date=2013-11-26\|Standardized application number=2013CA-2892325\|Event publication date=2014-06-05\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2892325\|Publication stage code=A1\|Publication date=2014-06-05\|Standardized publication number=CA2892325\|Event publication date=2018-01-26\|Event code=CA/EEER\|Event indicator=Pos\|Event group=Examination events\|Examination request\|Effective date of the event=2018-01-18\|Event publication date=2020-11-07\|Event code=CA/FZDE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Dead\|Effective date of the event=2020-08-31	(EP2925426)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP2925426)\|Extension States: ME, BA\|(WO2014/082996)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2014/082996)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2014/082996)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2014/082996)\|OAPI: KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2014/082996)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IR, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(WO2014/082996)\|MX\|(MX2015006607)\|MX	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=J4U2BTi8po23UZBNRU3cFKCa4vFyxJplNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US9631257&ekey=955&xpn=EP2925426&kind=A1	https://register.epo.org/application?number=EP13795508	https://permalink.orbit.com/RenderStaticFirstPage?XPN=E7lo66FogaTWqxLm4QBXD3fDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	EP	(WO2014/082996)\|FR	(WO2014/082996)\|NAME=LAFARGE 61 rue des Belles Feuilles F-75116 Paris , COUNTRY=FR	(EP2925426)\|FR\|\|(WO2014/082996)\|FR\|\|\|\|\|\|(AU2013351282)\|AU\|(AU2013351282)\|AU\|\|\|(CA2892325)\|CA	(EP2925426)\|NAME=Soares, Luis Filipe;Lafarge Group Intellectual Property 95, rue du Montmurier - BP9 , CITY=38291 Saint Quentin Fallavier Cedex , COUNTRY=FR , REG=101513670\|(US9631257)\|NAME=Pillsbury Winthrop Shaw Pittman LLP\|(WO2014/082996)\|NAME=MERIGEAULT, Shona Lafarge Propriété Intellectuelle Groupe 95 rue du Montmurier BP9 F-38291 Saint Quentin Fallavier Cedex , COUNTRY=FR\|(JP2015536897)\|NAME=MURAKOSHI, Satoshi , REG=100126572NAME=OBATA Yuichi , REG=100125195\|(CN104812468)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(CN104812468)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(RU2654983)\|NAME=LLC LAW FIRM GORODISSKY AND PARTNERS\|(RU2015125492)\|NAME=LLC LAW FIRM GORODISSKY AND PARTNERS\|(AU2013351282)\|NAME=Watermark Intellectual Property Pty Ltd L 1 109 Burwood Rd , CITY=Hawthorn , STATE=VIC , POSTCODE=3122 , COUNTRY=AU\|(AU2013351282)\|NAME=Watermark Patent and Trade Marks Attorneys 302 Burwood Road , CITY=Hawthorn , STATE=VIC , POSTCODE=3122 , COUNTRY=AU\|(MX2015006607)\|NAME=CARLOS PÉREZ DE LA SIERRA\|(KR10-2015-0088845)\|NAME=KOREANA PATENT FIRM , REG=920011000013\|(CA2892325)\|NAME=NORTON ROSE FULBRIGHT CANADA LLP/S.E.N.C.R.L., S.R.L. , COUNTRY=CA	(EP2925426)\|FR; FR; FR\|(US9631257)\|FR; FR; FR\|(US20150299823)\|FR; FR; FR\|(WO2014/082996)\|FR; FR; FR\|\|(CN104812468)\|FR\|\|(RU2654983)\|FR; FR; FR\|\|\|\|(MX2015006607)\|FR; FR; FR\|\|(CA2892325)\|FR; FR; FR	(EP2925426)\|NAME=PISCH, Alexander Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=F-38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=GARTNER, Ellis Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=F-38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=MEYER, Vincent Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=F-38291 Saint Quentin Fallavier, COUNTRY=FR\|(US9631257)\|NAME=Pisch Alexander, CITY=Saint Quentin Fallavier, COUNTRY=FR \|NAME=Gartner Ellis, CITY=Saint Quentin Fallavier, COUNTRY=FR \|NAME=Meyer Vincent, CITY=Saint Quentin Fallavier, COUNTRY=FR\|(US20150299823)\|NAME=PISCH Alexander, CITY=Saint Quentin Fallavier, COUNTRY=FR \|NAME=GARTNER Ellis, CITY=Saint Quentin Fallavier, COUNTRY=FR \|NAME=MEYER Vincent, CITY=Saint Quentin Fallavier, COUNTRY=FR\|(WO2014/082996)\|NAME=PISCH, Alexander Lafarge Centre de Recherche 95 Rue du Montmurier F-38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=GARTNER, Ellis Lafarge Centre de Recherche 95 Rue du Montmurier F-38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=MEYER, Vincent Lafarge Centre de Recherche 95 Rue du Montmurier F-38291 Saint Quentin Fallavier, COUNTRY=FR\|(JP2015536897)\|NAME=Pish, Alexander\|NAME=Gartner, Ellis\|NAME=Mayer, Vincent\|(CN104812468)\|NAME=PISCH ALEXANDER Paris, FRA, CITY=Paris, STATE=Paris , COUNTRY=FR \|NAME=E. Gartner\|NAME=V. Mayer\|(CN104812468)\|NAME=PISCH ALEXANDER\|NAME=GARTNER ELLIS\|NAME=MEYER VINCENT\|(RU2654983)\|NAME=PISH Aleksander, COUNTRY=FR \|NAME=GARTNER Ellis, COUNTRY=FR \|NAME=MEJER Vensan, COUNTRY=FR\|(RU2015125492)\|NAME=PISH ALEKSANDER\|NAME=GARTNER EHLLIS\|NAME=MEJER VENSAN\|(AU2013351282)\|NAME=Pisch, Alexander\|NAME=Gartner, Ellis\|NAME=Meyer, Vincent\|(AU2013351282)\|NAME=Pisch, Alexander\|NAME=Gartner, Ellis\|NAME=Meyer, Vincent\|(MX2015006607)\|NAME=ALEXANDER PISCH, COUNTRY=FR \|NAME=ELLIS GARTNER, COUNTRY=FR \|NAME=VINCENT MEYER, COUNTRY=FR\|(KR10-2015-0088845)\|NAME=PISCH ALEXANDER\|NAME=GARTNER ELLIS\|NAME=MEYER VINCENT\|(CA2892325)\|NAME=PISCH, ALEXANDER, COUNTRY=FR \|NAME=GARTNER, ELLIS, COUNTRY=FR \|NAME=MEYER, VINCENT, COUNTRY=FR	(WO2014/082996)\|2\|(AU2013351282)\|2\|(CN104812468)\|2\|(US9631257)\|2\|(JP2015536897)\|2\|\|(KR10-2015-0088845)\|2\|(CA2892325)\|2	4	10			(EP2925426)\|WO2014/082996\|(US9631257)\|WO2014/082996\|(JP2015536897)\|WO2014/082996\|(CN104812468)\|WO2014/082996\|(RU2654983)\|WO2014/082996\|(AU2013351282)\|WO2014/082996\|(MX2015006607)\|WO2014/082996\|(KR10-2015-0088845)\|WO2014/082996\|(CA2892325)\|WO2014/082996		(US9631257)\|Number of Claims: NCL=10\|Number of Drawings: NDR=1\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Dunn Colleen\|Art Unit.: ART =1736\|\|(US20150299823)\|Number of Claims: NCL=10\|Number of Drawings: NDR=1\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Dunn Colleen\|Art Unit.: ART =1736\|\|(WO2014/082996)\|Number of Claims: NCL=10\|Extended kind: EXTK=x\|\|(JP2015536897)\|Number of Claims: NCL=10\|Number of Pages: NPAGES=31\|Request for examination: REQEXA=false\|\|(CN104812468)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2017-08-25\|Gazette number: GAZNUM=33-3402\|Substantial examination effective date: 20151111 Examination duration: 21 months\|Number of Pages: NPAGES=20\|Primary examiner: Yang Bo\|Primary examiner: 杨波\|\|(CN104812468)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2015-07-29\|Gazette number: GAZNUM=31-30\|Substantial examination effective date: 20151111 Examination duration: 21 months\|Number of Pages: NPAGES=21\|Primary examiner: Yang Bo\|Primary examiner: 杨波\|\|(RU2654983)\|Number of Claims: NCL=14\|980 : 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры"\|\|(RU2015125492)\|Number of Claims: NCL=14\|980 : 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры"\|\|(AU2013351282)\|Number of Claims: NCL=9\|\|(AU2013351282)\|Number of Claims: NCL=8\|\|(MX2015006607)\|Number of Claims: NCL=10\|Number of Pages: NPAGES=58\|\|(KR10-2015-0088845)\|Number of Claims: NCL=10\|\|(CA2892325)\|Number of Claims: NCL=2\|Number of Pages: NPAGES=33\|	(US9631257)\|Previous publication: US20150299823 A1 2015-10-22 [US20150299823]\|(CN104812468)\|Previous publication: CN104812468 A 2015-07-29 [CN104812468]	(EP2925426)\|ENGLISH (ENG)	(RU2654983)\|Patent\|(AU2013351282)\|Patent\|(CN104812468B)\|Patent\|(US9631257)\|Patent\|(RU2015125492)\|Patent\|(JP2015536897)\|Patent\|(US20150299823)\|Patent\|(EP2925426)\|Patent\|(MX2015006607)\|Patent\|(KR20150088845)\|Patent\|(CN104812468)\|Patent\|(AU2013351282)\|Patent\|(CA2892325)\|Patent\|(WO201482996)\|Patent	Titre: (EP2925426)\|Process for the treatment of a silicate mineral Résumé: (EP2925426)\|The invention provides a process for the preparation of a second composition, said process comprising the steps of: -preparing a first compositioncomprising an alkali metal magnesium orthosilicate andoptionally either(i) magnesium oxide or(ii) an alkali metal silicate, byreaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R 2 O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO 2, being from 4:1 to 1:4, and -contacting the first composition with water to produce thesecond composition comprising an amorphous magnesium silicate hydrate (M-S-H). It is possible to isolateor producefurther useful products from the second composition.	41	Abstract	gpt-4o-mini	uncertain	The process involves silicate minerals and reactions with alkali metal carbonates, but it is unclear if the primary goal is carbon sequestration or enhanced weathering.

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#	Priority numbers	Application number	Publication numbers	Questel unique family ID (FAN)	Family publication details	Priority dates	Application dates	Publication dates	Grant dates	Expected expiry dates	Title	Abstract	Current assignees	Assignee history	Inventors	Inventors.1	Representative	Advantages / Previous drawbacks	Independent claims	Object of invention	Technical concepts	Claims	Description	English description	Keywords in context	Technology domains	CPC - Cooperative classification	CPC combinations groups	CPC History	IPC - International classification	IPC History	PCL - US patent classification	PCL History	Citing patents - Standardized publication number	Citing patents - Raw information	Cited patents - Standardized publication number	Cited patents - Raw information	Non-Latin cited patents	Standardized cited number	Cited non-patent literature	Family legal status	Legal status (Pending, Granted, Revoked, Expired, Lapsed)	Family legal state	Legal state (Alive, Dead)	Legal actions	Designated states	Protected authorities - Country codes	Original document	Image mosaics	National register site	Biblio summary	Earliest priority country	Assignee country	Assignee address	Representative country	Representative address	Inventor country	Inventor address	Number of figures	Number of priorities	Number of patents	Licensing interest name	Security interest name	WO parent publication number	EP parent application number	Notes	Filing details	Filing language	Document type	_text_to_classify	_source_row_index	_text_source	_model	is_relevant	justification	_error
1	CN202511707827	CN202511707827	CN121454002	117662153	CN121454002 A 2026-02-03 [CN121454002]	2025-11-20	2025-11-20	2026-02-03		(CN121454002)\|2045-11-20	(CN121454002)\|Leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions	(CN121454002)\|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, and belongs to the technical fields of rock weathering and carbon sequestration enhancement, mineral fertilizer development and saline soil improvement and treatment. The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions. The leaching equipment comprises a temperature control device, a leaching assembly, a rainfall simulation device, a temperature and humidity sensor and a controller, wherein the temperature control device comprises a support frame and a constant temperature box device arranged on the support frame. The leaching assembly comprises a leaching column arranged in the constant-temperature box device and a liquid collecting container arranged below the leaching column. The equipment can simulate a chemical weathering leaching experiment of silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment so as to really simulate a chemical weathering process of the silicate minerals in a natural environment of saline-alkali soil; scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners, novel mineral fertilizers and saline-alkali soil improvement.	LANZHOU UNIVERSITY\|MICROCARBON LOW CARBON TECHNOLOGY	(CN121454002)\|LANZHOU UNIVERSITY ([CN])\|Microcarbon (Guangzhou) Low Carbon Technology Co., Ltd.	ZHANG JIETANG\|LI XINGYUAN\|GOU XIAOHUA	(CN121454002)\|ZHANG JIETANG\|LI XINGYUAN\|GOU XIAOHUA	(CN121454002)\|HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP)\|Reg. Nb: 41028	(CN121454002)\|It will be appreciated that in some of these embodiments the first valve 9 and the second valve 10 are solenoid valves.\|The problems cause great deviation between laboratory simulated silicate mineral weathering experimental results and chemical weathering under actual natural conditions, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain.\|Based on the problem that the laboratory simulation silicate mineral weathering experimental result in the prior art has larger deviation from the chemical weathering under the actual natural condition, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain, the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions, which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable temperature and humidity conditions, so as to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and provide scientific basis and experimental support for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers.\|In practical researches, the following problems are common in the conventional silicate mineral chemical weathering leaching experimental device: (1) By adopting a manual liquid adding mode, the leaching solution amount is difficult to be matched with the natural precipitation condition;\|	(CN121454002)\|1. An leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, comprising: The temperature control device comprises a support frame and an incubator device arranged on the support frame; The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.\|	(CN121454002)\|In order to achieve the purpose, the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided, and comprises:\|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, and belongs to the technical fields of enhanced rock weathering carbon fixation, mineral fertilizer development and saline soil improvement and management.\|	(CN121454002)\|LEACHING COLUMN(100,88)\|POWDER(100,60)\|SILICATE(100,50)\|NATURAL TEMPERATURE(100,30)\|SIMULATING CHEMICAL WEATHERING(100,27)\|HUMIDITY CONDITION(100,16)\|LEACHING EQUIPMENT(100,7)\|SYNCHRONOUS PULLEY(77,6)\|RAINFALL SIMULATION(74,20)\|LINK ROD(71,15)\|LEACHING(65,36)\|INCUBATOR(54,39)\|CHEMICAL WEATHERING LEACHING EXPERIMENT(51,2)\|MULTIFUNCTIONAL SILICATE MINERAL DEVELOPMENT(49,3)\|LABORATORY SIMULATION SILICATE MINERAL(48,1)\|LEACHING EXPERIMENT(47,3)\|MULTIFUNCTIONAL SILICATE MINERAL(46,3)\|NUTRIENT RELEASE(44,2)\|HUMIDITY(41,34)\|RELIABLE SILICATE MINERAL(41,2)\|INJECTION CYLINDER(40,23)\|SIMULATED RAINFALL(39,5)\|COLUMNAR ROCK MASS(39,3)\|MINERAL FERTILIZER DEVELOPMENT(39,1)\|ENHANCED ROCK(38,1)\|LIQUID COLLECTION CONTAINER(35,10)\|SILICATE HUMIDITY(35,3)\|NATURAL RAINFALL(34,6)\|LINKAGE ROD(33,26)\|SALINE ALKALI SOIL(33,17)\|SALINE SOIL IMPROVEMENT(33,1)\|SEAT SUPPORT(32,17)\|SILICATE MINERAL(31,19)\|CIRCULATION AIR DUCT(31,5)\|CHEMICAL WEATHERING(28,18)\|NATURAL CONDITION(28,2)\|AIR CIRCULATION(24,15)\|CONTROLLABLE TEMPERATURE(24,3)\|HUMIDITY SENSOR(23,18)\|LEACHING SOLUTION(22,20)\|REFRIGERATOR(22,10)\|DRIVING PISTON(22,6)\|PUSH PULL ROD(21,17)\|MINERAL FERTILIZER(21,5)\|EXPERIMENTAL SUPPORT(20,4)\|LEACHING SOLUTION PUMPING(20,2)\|DEVIATION(20,1)\|THERMOSTAT(20,1)\|SILICATE TEMPERATURE(19,3)\|HUMIDITY ENVIRONMENT(19,2)\|LEACHING CHAMBER(19,2)\|SLIDING HOLE(18,6)\|SOIL TEMPERATURE(18,4)\|NATURAL PRECIPITATION CONDITION(18,2)\|LABORATORY(18,1)\|INFUSION TUBE(17,2)\|SILICATE MINERAL CHEMICAL WEATHERING(16,7)\|CONDITIONING AGENT(16,3)\|SPRAY BRACKET(16,3)\|HEAT PIPE(16,2)\|MESH PLATE(15,7)\|SILICATE RELATIVE HUMIDITY(14,3)\|LIQUID DELIVERY PIPE(14,2)\|SUPPORTING SPRAY(14,2)\|SYRINGE PUMP DRIVING(14,2)\|SOLENOID VALVE(14,1)\|LIQUID INLET(13,10)\|LIQUID OUTLET(13,10)\|LARGE DEVIATION(13,1)\|LIQUID ADDITION(13,1)\|SUPPORT FRAME(12,14)\|CIRCULATION DUCT(12,5)\|TEMPERATURE DETECTION(12,5)\|FILTER SCREEN(12,4)\|SYRINGE PUMP SUPPORT(12,3)\|LINK LEVER(11,9)\|CARBON FIXATION(11,4)\|NATURAL ENVIRONMENT(11,4)\|EQUAL LENGTH LINK ROD(11,3)\|DRIVING SHAFT(10,24)\|INJECTION PUMP(10,19)\|DRIVING LEVER(10,7)\|DRIVING MOTOR SHAFT(10,2)\|RAINFALL SIMULATOR(10,2)\|SUPPORT BASE(10,2)\|LEACHING COLUMN END(9,5)\|PRESET TEMPERATURE(9,5)\|SILICATE ROCK POWDER(9,2)\|EXPERIMENTAL SIMULATION AUTHENTICITY(9,1)\|LIQUID STORAGE CONTAINER(8,7)\|CHEMICAL WEATHERING SIMULATION EXPERIMENT(8,3)\|TIMING PULLEY(8,3)\|OPEN SHAPE(8,2)\|MULTIFUNCTIONAL SILICATE MINERAL CONDITIONER(8,1)\|DRIVING ROD(7,7)\|RELATIVE HUMIDITY(7,3)\|AIR RETURN OPENING(7,1)\|NUTRIENT SUPPLEMENTATION(7,1)\|REAL RAINFALL SIMULATION(7,1)\|SILICATE POWDER DISTURBANCE(7,1)\|GEAR(6,11)\|CARBON FIXING PROCESS DATA(6,3)\|SHOWER SOLUTION(6,3)\|SYNCHRONOUS BELT WHEEL(6,3)\|WATER INLET PIPE(6,3)\|DETECTING LEACHING LIQUID PRESSURE(6,2)\|HEATING AIR(6,2)\|NATURAL SALINE ALKALI SOIL(6,2)\|PRECIPITATION MINERAL CHEMICAL WEATHERING(6,2)\|RAINFALL SIMULATION DIAGRAM(6,2)\|RELIABLE WEATHERING REACTION(6,2)\|CONSTANT TEMPERATURE CAVITY INSIDE(6,1)\|LEACHING EXPERIMENT ACCURACY(6,1)\|RESEARCH SCIENTIFICITY(6,1)\|SALINE SOIL RECONSTRUCTION TREATMENT(6,1)\|SILICATE DISTURBANCE(6,1)\|SIMULATING LEACHING(6,1)\|PRESSURE SENSOR(5,7)\|AIR RETURN PIPE(5,4)\|INNER HOLE WALL(5,4)\|COLUMN ROCK MASS(5,2)\|TEMPERATURE REGULATION(5,2)\|TRANSFUSION TUBE(5,2)\|EXPERIMENTAL VERIFICATION(5,1)\|NOZZLE ATOMIZATION(5,1)\|OUTER CIRCUMFERENTIAL SURFACE(5,1)\|PAYING ATTENTION(5,1)\|PRECIPITATION SIMULATION(5,1)\|SALINE ALKALI SOIL HUMIDITY(5,1)\|SILICATE POWDER LEACHING SOLUTION(5,1)\|SUCKING LEACHING SOLUTION(5,1)\|TRANSPARENT OBSERVATION WINDOW(5,1)\|CONNECTING ROD(4,20)\|HEATING COMPONENT(4,5)\|CHEMICAL WEATHERING EXPERIMENT(4,2)\|HUMIDITY SENSOR FEED(4,2)\|INCUBATOR CONSTANT TEMPERATURE CAVITY(4,2)\|SPRAY COMPONENT(4,2)\|SPRAYING SUPPORT(4,2)\|SYRINGE DIRECTION(4,2)\|TRUE ACCURACY(4,2)\|1244 CIRCULATION FAN(4,1)\|ATOMIZING SPRAY HEAD(4,1)\|INCUBATOR HEATING(4,1)\|INSUFFICIENT NUTRIENT SUPPLY(4,1)\|LEACHING CAVITY(4,1)\|LEACHING SOLUTION CONCENTRATED IMPACT(4,1)\|LEACHING SOLUTION UNIFORMITY(4,1)\|PRESET HUMIDITY(4,1)\|CHAMBER DOOR(3,1)\|COLUMNAR ROCK TOP(3,1)\|CONSTANT TEMPERATURE INTRACAVITY REFRIGERATOR(3,1)\|HEAT PRESERVATION BOX(3,1)\|LEACHING COLUMN OPENING(3,1)\|MINERAL CONDITIONING AGENT DEVELOPMENT(3,1)\|MODIFIER(3,1)\|REAL SOIL CHANGE(3,1)\|	(CN121454002)\|1. An leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, comprising:\| The temperature control device comprises a support frame and an incubator device arranged on the support frame; \| The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; \| a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; \| a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and \|And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.\|2. The leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions according to claim 1, wherein the rainfall simulation device comprises a spraying assembly arranged at an opening at the top end of the leaching column, a syringe pump mechanism for drawing and pumping leaching solution, a liquid delivery pipe for connecting the spraying assembly and a liquid outlet port of the syringe pump mechanism, a water inlet pipe for connecting a liquid inlet port of the syringe pump mechanism with a liquid storage container, and a supporting seat for supporting the syringe pump mechanism, the syringe pump mechanism is fixedly arranged on the supporting seat, the leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions further comprises a driving device for driving the syringe pump mechanism to draw and pump leaching solution, a first valve arranged at the liquid inlet port of the syringe pump mechanism and a second valve arranged at the liquid outlet port of the syringe pump mechanism, the driving device is arranged on the supporting seat, and the controller can control the driving device, the first valve and the second valve to work, and the driving device and the second valve are respectively electrically connected with the controller.\|3. The leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 2, wherein the injection pump mechanism comprises an injection cylinder with two open ends, a first piston arranged in the injection cylinder in a sliding manner, a second piston arranged in the injection cylinder in a sliding manner, a push-pull rod for driving the first piston to move along the axial direction of the injection cylinder, a first linkage rod connected with one end of the push-pull rod far away from the first piston, a sleeve for driving the second piston to move along the axial direction of the injection cylinder, and a second linkage rod connected with one end of the sleeve far away from the second piston, wherein a first sliding hole for the push-pull rod to pass through is arranged on the second piston, the outer circumferential surface of the push-pull rod is in interference contact with the inner hole wall of the first sliding hole, the sleeve is sleeved on the rod in an axial sliding manner, and the first linkage rod and the second linkage rod are respectively connected with the driving device.\|4. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 3, wherein the driving means comprises a driving assembly, a link mechanism connecting the first link rod with the second link rod, and a gear mechanism connecting the link mechanism with the driving assembly, the gear mechanism comprising a first gear rotatably mounted on the support base and a second gear rotatably mounted on the support base, the first gear and the second gear being engaged, the first gear and/or the second gear being connected with the driving assembly so that the driving assembly can drive the first gear and the second gear to rotate synchronously, the link mechanism comprising a first link rod fixedly connected with the first gear, a first link rod rotatably connecting a first end of the first link rod with a first end of the first link rod, a second gear rotatably connecting a second end of the first link rod with a second end of the first link rod, a second gear fixedly connected with a second end of the second link rod, a second link rod of equal length, a second link rod rotatably connecting a second end of the second link rod with a second end of the second link rod, a second link rod of equal length, and a second link rod of equal length.\|5. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions of claim 4, wherein the driving assembly comprises a first driving shaft rotatably disposed on the supporting seat, a second driving shaft rotatably disposed on the supporting seat, a driving motor fixedly mounted on the supporting seat, a first synchronous pulley fixedly sleeved on the first driving shaft, a second synchronous pulley fixedly sleeved on the second driving shaft, a third synchronous pulley fixedly sleeved on a motor shaft of the driving motor, and a synchronous belt connecting the first synchronous pulley, the second synchronous pulley and the third synchronous pulley, wherein the driving motor is electrically connected with the controller.\|6. A leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 3, wherein a pressure sensor for detecting leaching liquid pressure in the injection cylinder is arranged in the injection cylinder, and the pressure sensor is electrically connected with the controller.\|7. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions of claim 1, wherein the leaching assembly further comprises a first mesh plate disposed in a leaching chamber within the leaching column and a first filter screen laid on the mesh plate, the silicate rock powder in the leaching column forming a columnar rock mass, a bottom end of the columnar rock mass being supported on the first mesh plate.\|8. The leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 1, wherein the incubator device comprises an incubator with a constant temperature cavity inside, a refrigerator arranged on the incubator to selectively open or close the constant temperature cavity, a refrigerator arranged inside the incubator to realize temperature regulation in the constant temperature cavity, and an air circulation and heating mechanism arranged inside the incubator, wherein the air circulation and heating mechanism can accelerate air circulation flow in the constant temperature cavity and heat air in the constant temperature cavity, the controller can control the refrigerator and the air circulation and heating mechanism to work according to humidity and temperature detected by the temperature and humidity sensor, and the temperature in the constant temperature cavity is regulated so as to keep the temperature in the constant temperature cavity within a preset temperature range of 0-25 ℃.\|9. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to claim 8, wherein the air circulation and heat supply mechanism comprises a circulation air duct arranged in the constant temperature cavity, an air inlet pipe communicated with an air inlet of the circulation air duct, an air return pipe communicated with an air return opening of the circulation air duct, a heating assembly arranged in the circulation air duct, and a circulation fan arranged in the circulation air duct, and the heating assembly comprises a plurality of heating pipes which are transversely arranged.\|10. The leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to any one of claims 2 to 6, wherein the spray assembly comprises a spray head connected to the infusion tube and a spray bracket for supporting the spray head on the support frame and/or at the top end of the leaching column, the spray bracket being detachably connected to the support frame and/or the leaching column.	(CN121454002)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction treatment, and particularly relates to leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions.\|BACKGROUND ART\|[0002] The saline-alkali soil has the problems of deterioration of physical and chemical properties of soil, insufficient nutrient supply, limited plant growth and the like due to high salt content and strong alkalinity.\|[0003] The conventional saline-alkali soil improvement methods comprise salt removal, salt pressing, organic fertilizer application, chemical modifier application and the like, but the methods have the defects of slow effect, high cost, high environmental risk or difficult long-term maintenance of improvement effect and the like. In recent years, mineral fertilizers have been greatly developed in the aspect of saline-alkali soil improvement, silicate minerals are utilized for weathering to release nutrient elements such as calcium, magnesium, potassium, phosphorus and the like, carbonate minerals are formed by reaction with atmospheric carbon dioxide, and research on soil improvement, nutrient supplementation, carbon fixation and sink increase is increasingly paid attention to. However, the existing research is still imperfect in simulating leaching and chemical weathering rules of silicate minerals under the conditions of natural precipitation and soil temperature and humidity, and lacks experimental verification and model support of a system. In practical researches, the following problems are common in the conventional silicate mineral chemical weathering leaching experimental device:\| (1) By adopting a manual liquid adding mode, the leaching solution amount is difficult to be matched with the natural precipitation condition; \| (2) Only is carried out at room temperature, lacks heating and temperature control functions, and cannot reflect the change of the real soil under the temperature and humidity conditions. \|[0004] The problems cause great deviation between laboratory simulated silicate mineral weathering experimental results and chemical weathering under actual natural conditions, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain. Therefore, development of a chemical weathering leaching experimental device capable of simulating silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment is needed to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners and novel mineral fertilizers.\|DISCLOSURE\|Disclosure of Invention\|[0005] Based on the problem that the laboratory simulation silicate mineral weathering experimental result in the prior art has larger deviation from the chemical weathering under the actual natural condition, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain, the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions, which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable temperature and humidity conditions, so as to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and provide scientific basis and experimental support for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers.\|[0006] In order to achieve the purpose, the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided, and comprises:\| The temperature control device comprises a support frame and an incubator device arranged on the support frame; \| The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; \| a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; \| a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and \|And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.\|[0007] Further, the rainfall simulation device comprises a spraying component arranged at the open top of the leaching column, a syringe pump mechanism for drawing and pumping leaching solution, a liquid delivery pipe for connecting the spraying component with a liquid outlet port of the syringe pump mechanism, a water inlet pipe for connecting a liquid inlet port of the syringe pump mechanism with a liquid storage container, and a supporting seat for supporting the syringe pump mechanism, wherein the syringe pump mechanism is fixedly arranged on the supporting seat, the leaching device for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity further comprises a driving device for driving the syringe pump mechanism to draw and pump leaching solution, a first valve arranged at the liquid inlet port of the syringe pump mechanism and a second valve arranged at the liquid outlet port of the syringe pump mechanism, the driving device is arranged on the supporting seat, and the driving device, the first valve and the second valve can be controlled to work and are respectively and electrically connected with the controller.\|[0008] Further, the injection pump mechanism comprises an injection cylinder, a first piston, a second piston, a push-pull rod, a first linkage rod, a sleeve and a second linkage rod, wherein the two ends of the injection cylinder are respectively in an opening shape, the first piston is arranged in the injection cylinder in a sliding mode, the second piston is arranged in the injection cylinder in a sliding mode, the push-pull rod is used for driving the first piston to move along the axial direction of the injection cylinder, the first linkage rod is connected with one end, far away from the first piston, of the push-pull rod, the sleeve is used for driving the second piston to move along the axial direction of the injection cylinder, the second linkage rod is connected with one end, far away from the second piston, of the sleeve, a first sliding hole is formed in the second piston, the outer peripheral surface of the push-pull rod is in interference contact with the inner hole wall of the first sliding hole, the sleeve can be sleeved on the push-pull rod in an axial sliding mode, and the first linkage rod and the second linkage rod are respectively connected with the driving device.\|[0009] Further, the driving device comprises a driving assembly, a connecting rod mechanism connecting the first linkage rod with the second linkage rod, and a gear mechanism connecting the connecting rod mechanism with the driving assembly, wherein the gear mechanism comprises a first gear rotatably installed on the supporting seat and a second gear rotatably installed on the supporting seat, the first gear is meshed with the second gear, the first gear and/or the second gear are/is connected with the driving assembly so that the driving assembly can drive the first gear and the second gear to synchronously rotate, the connecting rod mechanism comprises a first driving rod fixedly connected with the first gear, a first connecting rod rotatably connecting the first end of the first driving rod with the first end of the first linkage rod, a second connecting rod rotatably connecting the second end of the first driving rod with the first end of the second linkage rod, a second driving rod fixedly connected with the second gear, a second connecting rod fixedly connected with the second end of the second driving rod, a second connecting rod fixedly connected with the second end of the second connecting rod, a second connecting rod with the second connecting rod, and a first connecting rod with the second connecting rod, and a second connecting rod with the second connecting rod, and the connecting rod with the second connecting rod with the first connecting rod and the second connecting rod with the second connecting rod.\|[0010] Further, the driving assembly comprises a first driving shaft arranged on the supporting seat in a rotating mode, a second driving shaft arranged on the supporting seat in a rotating mode, a driving motor fixedly installed on the supporting seat, a first synchronous belt wheel fixedly sleeved on the first driving shaft, a second synchronous belt wheel fixedly sleeved on the second driving shaft, a third synchronous belt wheel fixedly sleeved on a motor shaft of the driving motor, and a synchronous belt connecting the first synchronous belt wheel, the second synchronous belt wheel and the third synchronous belt wheel, wherein the driving motor is electrically connected with the controller.\|[0011] Further, a pressure sensor for detecting the leaching solution pressure in the injection cylinder is arranged in the injection cylinder, and the pressure sensor is electrically connected with the controller.\|[0012] Further, the leaching assembly further comprises a first mesh plate arranged in a leaching cavity in the leaching column and a first filter screen paved on the mesh plate, silicate rock powder in the leaching column forms a columnar rock body, and the bottom end of the columnar rock body is supported on the first mesh plate.\|[0013] Further, the incubator device includes the incubator that inside was equipped with the constant temperature chamber, set up in on the incubator in order to open or close selectively the chamber door in constant temperature chamber, set up in inside in order to realize the refrigerator of constant temperature intracavity temperature regulation of incubator, and set up in inside air cycle and the heating mechanism of incubator, air cycle and the heating mechanism can be accelerated air cycle flow in the constant temperature chamber, and heat air in the constant temperature chamber, the controller can be according to humidity and the temperature control that temperature and humidity sensor detected the refrigerator air cycle and the heating mechanism work, adjust the temperature in the constant temperature chamber, so that the temperature in the constant temperature chamber keeps in the preset temperature range of 0 ℃ to 25 ℃.\|[0014] Further, the air circulation and heat supply mechanism comprises a circulation air channel arranged in the constant temperature cavity, an air inlet pipe communicated with an air inlet of the circulation air channel, an air return pipe communicated with an air return port of the circulation air channel, a heating component arranged in the circulation air channel and a circulation fan arranged in the circulation air channel, wherein the heating component comprises a plurality of heating pipes which are transversely arranged.\|[0015] Further, the spraying assembly comprises a spray head connected with the infusion tube and a spraying support for supporting the spray head on the support frame and/or at the top end of the leaching column, and the spraying support is detachably connected with the support frame and/or the leaching column.\|[0016] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:\| According to the leaching equipment for simulating chemical weathering under the natural temperature and humidity conditions of silicate rock powder, which is disclosed by the embodiment of the invention, the actual natural rainfall and the natural saline-alkali soil temperature and humidity conditions can be simulated, and mineral chemical weathering of the precipitation amount is simulated according to the actual temperature and humidity of the saline-alkali soil, so that the chemical weathering process of silicate minerals in the natural environment of the saline-alkali soil is simulated truly, the true accuracy of the silicate mineral chemical weathering experimental result is improved, and the reliable weathering reaction, salt replacement and carbon fixing process data of the silicate minerals in the saline-alkali soil are obtained, so that scientific basis and experimental support are provided for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers. \|DRAWINGS DESCRIPTION\|[0017] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0018] FIG. 1 is a schematic diagram of a three-dimensional structure of leaching equipment simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions;\| FIG. 2 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 3 is a schematic top view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 4 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 5 is an assembly diagram of a rainfall simulation device and a driving device according to an embodiment of the present invention in a first working state; \| FIG. 6 is a schematic cross-sectional view of the structure shown in FIG. 5; \| fig. 7 is an assembly diagram of the rainfall simulation device and the driving device provided by the embodiment of the invention in a second working state; \| FIG. 8 is a schematic top view of the structure shown in FIG. 7; \| FIG. 9 is a schematic cross-sectional view of the structure shown in FIG. 7; \| Fig. 10 is a schematic perspective view of a leaching assembly according to an embodiment of the present invention; \| FIG. 11 is a schematic cross-sectional view of a leaching assembly according to an embodiment of the present invention; \| FIG. 12 is an exploded view of a leaching assembly provided by an embodiment of the present invention; \| FIG. 13 is a schematic perspective view of an incubator assembly according to an embodiment of the present invention; \| Fig. 14 is a schematic cross-sectional structure of an incubator assembly according to an embodiment of the present invention. \|[0019] Wherein, each reference sign in the figure:\| 1-temperature control device, 11-supporting frame, 12-incubator device, 121-incubator, 122-oven door, 123-refrigerator, 124-air circulation and heat supply mechanism, 1241-circulation air duct, 1242-muffler, 1243-heating assembly, 1244-circulation fan, 1245-air inlet pipe, 125-mounting hole and 126-observation window; \| 2-leaching components, 21-leaching columns, 22-liquid collecting containers, 23-liquid discharge pipes, 24-first mesh plates, 25-first filter screens, 26-second filter screens and 27-second mesh plates; \| 3-a rainfall simulation device, 31-a spray assembly, 311-a spray head, 312-a spray bracket, 32-a syringe pump mechanism, 321-a syringe, 322-a first piston, 323-a second piston, 324-a push-pull rod, 325-a first linkage rod, 326-a sleeve, 327-a second linkage rod, 33-a transfusion tube, 34-a water inlet tube and 35-a supporting seat; \| 4-drive means, 41-drive assembly, 411-first drive shaft, 412-second drive shaft, 413-drive motor, 414-first timing pulley, 415-second timing pulley, 416-third timing pulley, 417-timing belt, 418-motor shaft, 42-link mechanism, 421-first drive rod, 422-first link, 423-second link, 424-second drive rod, 425-third link, 426-fourth link, 43-gear mechanism, 431-first gear, 432-second gear; \| 5-fixed support, 6-bolt piece, 7-liquid storage space, 8-columnar rock mass and 9-controller. \|INVENTION MODE\|Detailed Description\|[0020] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0021] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, features defining "first," "second," and "third" may explicitly or implicitly include one or more such features. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0022] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.\|[0023] Referring to fig. 1 to 14, a description will now be given of an leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention. Referring to fig. 1, fig. 2, fig. 3 and fig. 4 in combination, the leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions provided by the embodiment of the invention comprises a temperature control device 1, a leaching assembly 2, a rainfall simulation device 3, a temperature and humidity sensor and a controller 9, wherein the temperature control device 1 comprises a support frame 11 and a constant temperature box device 12 arranged on the support frame 11. The leaching assembly 2 comprises a leaching column 21 arranged in the incubator device 12 and a liquid collecting container 22 arranged below the leaching column 21, wherein two axial ends of the leaching column 21 respectively extend out of the incubator device 12, the top end of the leaching column 21 is open, and a liquid discharging pipe 23 communicated with the liquid collecting container 22 is arranged at the bottom end of the leaching column 21. Wherein, the leaching column 21 is a column-shaped leaching container made of high-temperature resistant transparent plastic or high-temperature resistant transparent organic glass. The rainfall simulation device 3 is used for simulating rainfall so that the leaching solution can uniformly flow into silicate rock powder in the leaching column 21 through the top end opening of the leaching column 21. The temperature and humidity sensor is used for detecting the temperature and humidity of silicate rock powder in the leaching column 21 in real time, and a probe of the temperature and humidity sensor is inserted into the leaching column 21. It should be noted that, the temperature and humidity sensor is implemented by adopting the prior art, and its working principle and structure are well known to those skilled in the art, and are not described herein. The controller 9 is used for controlling the rainfall simulation device 3 and the incubator device 12 to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of the silicate rock powder in the leaching column 21 is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column 21 is maintained at 30-80%. It should be noted that the controller 9 may be, but is not limited to, a programmable logic controller.\|[0024] The basic working principle of the leaching equipment for simulating chemical weathering of silicate rock powder under the natural temperature and humidity condition is that silicate rock is crushed into silicate rock powder with the particle size of 0.1 micron, the silicate rock powder and a certain amount of saline-alkali soil are uniformly mixed and filled in a leaching column 21 of a leaching assembly 2, and a rainfall simulation device 3 is arranged at the opening at the top end of the leaching column 21. The simulated rainfall device 3 carries out real simulated rainfall characteristics on the leaching solution, so that the leaching solution can flow into the silicate rock powder in the leaching column 21 through the opening at the top end of the leaching column 21, the silicate rock powder in the leaching column 21 can be uniformly leached, disturbance on the silicate rock powder in the leaching column 21 is reduced, leaching efficiency and leaching effect of the silicate rock powder in the leaching column 21 are improved, and accuracy of silicate mineral chemical weathering experimental results is improved. In addition, during leaching, the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, and after the leaching solution permeates the silicate rock powder in the leaching column 21, the leaching solution is drained into the liquid collecting container 22 through the liquid drain pipe 23 at the bottom end of the leaching column 21. And, in the whole process of the chemical weathering experiment, the temperature in the incubator device 1 and the humidity in the leaching column 21 are detected in real time through the temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is less than 0 ℃, the controller 9 controls the heating component in the incubator device 1 to heat and work until the temperature in the incubator device 1 reaches 25 ℃, and the controller 9 controls the heating component in the incubator device 1 to stop heating and work. When the temperature in the oven apparatus 1 is greater than 25 ℃, the controller 9 controls the refrigerator in the oven apparatus 1 to operate until the temperature in the oven apparatus 1 reaches 25 ℃, and the controller 9 controls the refrigerator in the oven apparatus 1 to stop the cooling operation. The circulation is such that the temperature in the oven apparatus 1 is controlled within a preset temperature range of 0 to 25 ℃, thereby making the silicate rock powder in the leaching column 21 subjected to the chemical weathering simulation experiment under the temperature condition of 0 to 25 ℃. Of course, the controller 9 may also control the operation of the heating element and/or the refrigerator in the incubator apparatus 1 so that the temperature in the incubator apparatus 1 is stabilized at any one of the preset temperature values between 0 ℃ and 25 ℃ and so that the silicate powder in the leaching column 21 is subjected to chemical weathering simulation test under a specific temperature condition (e.g., 5 ℃, 10 ℃, 15 ℃, 20 ℃,25 ℃ or the like) between 0 ℃ and 25 ℃. Meanwhile, when the humidity in the leaching column 21 is less than 30%, the controller 9 controls the rainfall simulation device 3 to work, so that the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, until the humidity in the leaching column 21 reaches 80%, the controller 9 controls the rainfall simulation device 3 to stop working, and the circulation is performed in such a way that the humidity in the leaching column 21 is controlled within a preset humidity range of 30-80%, and thus chemical weathering simulation experiments are performed on the silicate rock powder in the leaching column 21 under a humidity condition of 30-80%. Therefore, the method can simulate the actual natural rainfall and the natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, simulate the mineral chemical weathering of the precipitation according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and improve the true accuracy of the silicate mineral chemical weathering experimental result so as to obtain the reliable weathering reaction, salt replacement and carbon fixation process data of the silicate minerals of the saline-alkali soil, thereby being beneficial to improving the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|[0025] Referring to fig. 2,3 and 4, in some embodiments, the rainfall simulation device 3 includes a spray assembly 31 disposed at an opening at a top end of the leaching column 21, a syringe pump mechanism 32 for drawing and pumping the leaching solution, a transfusion tube 33 connecting the spray assembly 31 and a liquid outlet port of the syringe pump mechanism 32, a water inlet pipe 34 for connecting a liquid inlet port of the syringe pump mechanism 32 with a liquid storage container, and a support seat 35 for supporting the syringe pump mechanism 32, the syringe pump mechanism 32 is fixedly mounted on the support seat 35, the leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions further includes a driving device 4 for driving the syringe pump mechanism 32 to draw and pump the leaching solution, a first valve disposed at the liquid inlet port of the syringe pump mechanism 32 and a second valve disposed at the liquid outlet port of the syringe pump mechanism 32, the driving device 4 is disposed on the support seat 35, and the controller 9 can control the driving device 4, the first valve and the second valve to work, and the driving device 4, the first valve and the second valve are respectively electrically connected with the controller 9. It will be appreciated that in some of these embodiments the first valve 9 and the second valve 10 are solenoid valves. By the above arrangement, the silicate rock is crushed into silicate rock powder having a particle size of 0.1 μm, the silicate rock powder is packed in the leaching column 21 of the leaching assembly 2, and the spraying assembly 31 is installed at the top end opening of the leaching column 21. When the injection pump mechanism 32 is required to be used for sucking the leaching solution from the liquid storage container under the negative pressure, the controller controls the first valve 9 to open the liquid inlet of the injection pump mechanism 32, the controller controls the second valve 10 to close the liquid outlet of the injection pump mechanism 32, the driving device 4 drives the injection pump mechanism 32 to suck the leaching solution from the liquid storage container under the negative pressure, until the leaching solution in the injection pump mechanism 32 is full, the controller controls the first valve 9 to close the liquid inlet of the injection pump mechanism 32, and the controller controls the second valve 10 to open the liquid outlet of the injection pump mechanism 32, the injection pump mechanism 32 can pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the simulated rainfall device 3 under the driving action of the driving device 4, the real rainfall simulation characteristic is realized, the uniformity of the silicate powder in the leaching column 21 is ensured, the silicate powder in the leaching column 21 is uniformly leached, the disturbance of the silicate powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate powder in the leaching column 21 are further improved, and the accuracy of silicate mineral chemical weathering experiment results is facilitated. In addition, during leaching, the leaching solution of the silicate powder in the leaching column 21 is uniformly sprayed to the leaching column 21 at a certain flow rate through the spraying assembly 31, and is drained into the liquid collecting container 22 through the drain pipe 23 at the bottom end of the leaching column 21 after penetrating the silicate powder in the leaching column 21.\|[0026] Therefore, in the leaching device for simulating chemical weathering of silicate rock powder under the natural temperature and humidity conditions, when the controller controls the first valve 9 to be opened and the second valve 10 to be closed, the driving device 4 can drive the injection pump mechanism 32 to draw the leaching solution from the liquid storage container through negative pressure until the injection pump mechanism 32 draws enough leaching solution, then the controller controls the first valve 9 to be closed and the second valve 10 to be opened, the injection pump mechanism 32 can continuously pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the rainfall simulator 3 under the driving action of the driving device 4, the real rainfall simulation characteristic of the spraying assembly 31 of the rainfall simulator 3 is adopted to ensure the uniformity of the leaching solution flowing into the silicate rock powder in the leaching column 21, so that the silicate rock powder in the leaching column 21 can be uniformly leached, the disturbance of the silicate rock powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate rock powder in the leaching column 21 are improved, and the accuracy of the silicate mineral chemical weathering experiment result is improved.\|[0027] Referring to fig. 2,6 and 9 in combination, in some embodiments, the syringe pump mechanism 32 includes a syringe 321, a first piston 322, a second piston 323, a push-pull rod 324, a first linkage rod 325, a sleeve 326 and a second linkage rod 327, two ends of the syringe 321 are all open, the first piston 322 and the second piston 323 are respectively slidably disposed in the syringe 321, and when the first piston 322 and the second piston 323 are respectively slid to the openings at two ends of the syringe 321, a closed liquid storage space 7 for storing the shower solution can be formed in the syringe 321, and the liquid storage capacity of the liquid storage space 7 can be preset. The push-pull rod 324 is used for driving the first piston 322 to move along the axial direction of the injection cylinder 321, the sleeve 326 is used for driving the second piston 323 to move along the axial direction of the injection cylinder 321, and when the first piston 322 and the second piston 323 move away from each other along the axial direction of the injection cylinder 321, the solution can be pumped from the liquid storage container through the injection pump mechanism 32, and the pumped solution can be stored in the closed liquid storage space 7 between the first piston 322 and the second piston 323. When the first piston 322 and the second piston 323 move closer to each other in the axial direction of the syringe 321, the shower solution in the solution storage space 7 can be continuously pumped to the shower assembly 31 of the rainfall simulation device 3 by the syringe pump mechanism 32. The first linkage rod 325 is connected with one end of the push-pull rod 324 far away from the first piston 322, the second linkage rod 327 is connected with one end of the sleeve 326 far away from the second piston 323, the first linkage rod 325 and the second linkage rod 327 are respectively connected with the driving device 4, a first sliding hole for the push-pull rod 324 to pass through is arranged on the second piston 323, the outer peripheral surface of the push-pull rod 324 is in interference contact with the inner hole wall of the first sliding hole, and the sleeve 326 can be sleeved on the push-pull rod 324 in an axial sliding manner. When the driving device 4 drives the first linkage rod 325 and the second linkage rod 327, the sleeve 326 is sleeved on the push-pull rod 324 in a sliding manner along the axial direction, so that the first piston 322 and the second piston 323 can move towards or away from each other along the axial direction of the injection cylinder 321. It should be noted that, the liquid inlet port and the liquid outlet port are both disposed on the syringe 321, and the liquid inlet port and the liquid outlet port are respectively communicated with the liquid storage space 7.\|[0028] Referring to fig. 4, 5, 7 and 8 in combination, in some embodiments, the driving device 4 includes a driving assembly 41, a link mechanism 42 and a gear mechanism 43, the link mechanism 42 is used to connect the first link lever 325 with the second link lever 327, the gear mechanism 43 is used to connect the link mechanism 42 with the driving assembly 41, the gear mechanism 43 includes a first gear 431 rotatably mounted on the support seat 35 and a second gear 432 rotatably mounted on the support seat 35, the first gear 431 and the second gear 432 are the same in size and structure, the first gear 431 and the second gear 432 mesh, the first gear 431 and the second gear 432 are connected with the driving assembly 41, and one gear of the first gear 431 and the second gear 432 may be connected with the driving assembly 41, so that the driving assembly 41 can drive the first gear 431 and the second gear 432 to rotate synchronously. The link mechanism 42 includes a first driving lever 421 fixedly coupled to a first gear 431, a first link 422 rotatably coupling a first end of the first driving lever 421 with a first end of a first link lever 325, a second link 423 rotatably coupling a second end of the first driving lever 421 with a first end of a second link lever 327, a second driving lever 424 fixedly coupled to a second gear 432, a third link 425 rotatably coupling a first end of the second driving lever 424 with a second end of the first link lever 325, a fourth link 426 rotatably coupling a second end of the second driving lever 424 with a first end of the second link lever 327, the lengths of the first link 422, the second link 423, the third link 425, and the fourth link 426 being equal, the length of the first link lever 325 being equal to the length of the second link lever 327, and the length of the first driving lever 421 being equal to the length of the second link lever 424. It should be noted that, two ends of the first link 422 are respectively rotatably connected to the first end of the first driving rod 421 and the first end of the first linkage rod 325 through a pivot, and two ends of the second link 423 are respectively rotatably connected to the second end of the first driving rod 421 and the second end of the first linkage rod 325 through a pivot. Through the above structure, the driving assembly 41 can synchronously drive the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321, and can improve the stability of the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321. In addition, the connecting rod mechanism 42 is driven by the rotation of the gear mechanism 43 to drive the first piston 322 and the second piston 323 to move close to each other along the axial direction of the injection cylinder 321, and the speed of the injection pump mechanism 32 for pumping the leaching solution can be controlled by controlling the rotation speed of the first gear 431 and/or the second gear 432, so that the leaching rate can be controlled and regulated according to the leaching experiment requirement.\|[0029] Referring to fig. 4, 5 and 7, in some embodiments, the driving assembly 41 includes a first driving shaft 411, a second driving shaft 412, a driving motor 413, a first synchronous belt 417 wheel 414, a second synchronous belt 417 wheel 415, a third synchronous belt 417 wheel 416 and a synchronous belt 417, the first driving shaft 411 and the second driving shaft 412 are respectively rotatably disposed on the supporting seat 35, the driving motor 413 is fixedly mounted on the supporting seat 35, the first synchronous belt 417 wheel 414 is fixedly sleeved on the first driving shaft 411, the second synchronous belt 417 wheel 415 is fixedly sleeved on the second driving shaft 412, the third synchronous belt 417 wheel 416 is fixedly sleeved on a motor shaft 418 of the driving motor 413, and the synchronous belt 417 connects the first synchronous belt 417 wheel 414, the second synchronous belt 417 wheel 415 and the third synchronous belt 417 wheel 416, and the driving motor 413 is electrically connected with the controller. Through the above structure arrangement, under the driving action of the driving motor 413, the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 synchronously rotate, so as to drive the gear mechanism 43 to rotate, and the gear mechanism 43 drives the first piston 322 and the second piston 323 to move close to or far away from each other along the axial direction of the injection cylinder 321 through the link mechanism 42, so that the injection pump mechanism 32 can finish the action of drawing and pumping the shower solution.\|[0030] Referring to fig. 2, 4 and 5, in some embodiments, the first gear 431 is fixedly sleeved on the first driving shaft 411, the second gear 432 is fixedly sleeved on the second driving shaft 412, and the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are arranged in an isosceles triangle, so that the distance between the first driving shaft 411 and the second driving shaft 412, the distance between the first driving shaft 411 and the motor shaft 418 of the driving motor 413, and the distance between the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are all equal. By the above arrangement, the stability of the movement of the first piston 322 and the second piston 323 in the axial direction of the syringe 321 toward each other or away from each other can be improved.\|[0031] In some embodiments, a pressure sensor for detecting leaching liquid pressure inside the syringe 321 is disposed in the syringe 321, and the pressure sensor is electrically connected to the controller. The controller can control the rotation speed of the driving motor 413 to control the rotation speed of the first gear 431 and/or the second gear 432 according to the pressure detected by the pressure sensor, so as to control the speed of the injection pump mechanism 32 for pumping the leaching solution, thereby being convenient for controlling and adjusting the leaching rate according to the leaching experiment requirement.\|[0032] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a first mesh plate 24 disposed in the leaching chamber in the leaching column 21 and a first filter screen 25 laid on the mesh plate, silicate rock powder in the leaching column 21 forms a columnar rock body 8, and a bottom end of the columnar rock body 8 is supported on the first mesh plate 24. Through the structure setting, through adopting the first mesh board 24 that plastics or metal etc. made to the silicate rock powder in the leaching column 21 to form column rock mass 8 bottom formation support, the leaching solution after the rethread first filter screen 25 on the first mesh board 24 filters, can prevent effectively that the silicate rock powder in the leaching column 21 from forming column rock mass 8 bottom and collapsing, ensure simultaneously that the leaching solution that liquid collecting container 22 collected does not contain silicate rock powder, be favorable to improving the accuracy of leaching experiment. The mesh size of the first screen 25 is smaller than the particle size of the silicate powder.\|[0033] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a second screen 26 disposed on top of the columnar rock mass 8 and a second mesh plate 27 disposed over the second screen 26. By paving the second filter screen 26 on the top end of the columnar rock body 8 formed by silicate rock powder in the leaching column 21 and covering the second filter screen 26 with a second mesh plate 27 made of hard materials such as plastics or metals, the integrity of the top of the columnar rock body 8 is prevented from being damaged due to the fact that the concentrated impact of leaching solution water flows form a dent.\|[0034] Referring to fig. 2 and 4 in combination, in some embodiments, spray assembly 31 includes a spray head 311 coupled to a fluid line 33, and a spray bracket 312 for supporting spray head 311 on support frame 1 and/or on the top of leaching column 21, spray bracket 312 being removably coupled to support frame 1 and/or leaching column 21. It should be noted that the spray head 311 may be, but is not limited to, an atomizing spray head 311. In actual operation, the speed of the driving motor 413 is controlled, and various rainfall is simulated by adopting the atomizing nozzle 311, so that silicate rock powder in the leaching column 21 forms a columnar rock body 8, and the problems that the soil column structure is damaged and the leaching speed of water is influenced due to the fact that water flow impacts to form a recess are avoided.\|[0035] Referring to fig. 13 and 14 in combination, in some embodiments, the incubator apparatus 12 includes an incubator 121 having a constant temperature chamber therein, a door 122 provided on the incubator 121 to selectively open or close the constant temperature chamber, a refrigerator 123 provided inside the incubator 121 to achieve temperature adjustment in the constant temperature chamber, and an air circulation and heat supply mechanism 124 provided inside the incubator 121, the air circulation and heat supply mechanism 124 being capable of accelerating the air circulation flow in the constant temperature chamber and heating the air in the constant temperature chamber, and the controller 9 being capable of controlling the operation of the refrigerator 123, the air circulation and heat supply mechanism 124 according to the humidity and temperature detected by the temperature and humidity sensor to adjust the temperature in the constant temperature chamber so as to maintain the temperature in the constant temperature chamber within a preset temperature range of 0 to 25 ℃ or to any specific temperature value between 0 to 25 ℃. The incubator 121 is provided with a mounting hole 125 for accommodating and mounting the leaching column 21, and the outer side wall of the leaching column 21 is in airtight contact with the inner hole wall of the mounting hole 125. The door 122 is provided with a transparent observation window 126 made of high temperature resistant glass so as to observe leaching conditions in the leaching column 21 inside the incubator 121. In the whole process of chemical weathering experiment, the temperature in the incubator device 1 is detected in real time through a temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is smaller than 0 ℃, the controller 9 controls the refrigerator 123 to be closed and controls the air circulation and heat supply mechanism 124 in the heat preservation 121 to work, and the air circulation and heat supply mechanism 124 accelerates the air circulation flow in the constant temperature cavity and heats the air in the constant temperature cavity, so that the temperature in the constant temperature cavity of the incubator 121 is quickly increased until the temperature in the constant temperature cavity of the incubator 121 reaches 25 ℃, and the controller 9 controls the air circulation and heat supply mechanism 124 in the incubator device 1 to stop heating work. If the temperature in the constant temperature chamber of the incubator 121 is higher than 25 ℃, the controller 9 controls the refrigerator 123 to operate and controls the air circulation and heating mechanism 124 to stop operating, so that the temperature in the constant temperature chamber is reduced by between 0 and 25 ℃. By means of the circulation, the temperature in the heat preservation box 121 can be controlled within a preset temperature range of 0-25 ℃, so that silicate rock powder in the leaching column 21 is subjected to chemical weathering simulation experiments under the temperature condition of 0-25 ℃ to simulate actual natural rainfall and natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, mineral chemical weathering of simulated precipitation is performed according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and the actual accuracy of silicate mineral chemical weathering experiment results is improved.\|[0036] Referring to fig. 13 and 14 in combination, in some embodiments, the air circulation and heat supply mechanism 124 includes a circulation duct 1241 disposed in the constant temperature chamber, an air inlet pipe 1245 connected to an air inlet of the circulation duct 1241, an air return pipe 1242 connected to an air return port of the circulation duct 1241, a heating assembly 1243 disposed in the circulation duct 1241, and a circulation fan 1244 disposed in the circulation duct 1241, the heating assembly 1243 including a plurality of heating pipes disposed transversely. When the air circulation and heat supply mechanism 124 works, air in the constant temperature cavity is led into the circulation air channel 1241 by the air inlet pipe 1245 under the action of the circulation fan 45, the air in the circulation air channel 1241 is heated by the heating component 1244 and then becomes hot air, and the hot air in the circulation air channel 1241 flows back to the constant temperature cavity by the air return pipe 1243, so that the air circulation and heat supply mechanism 124 can be used for quickly heating the air in the constant temperature cavity.\|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.	(CN121454002)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction treatment, and particularly relates to leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions.\|BACKGROUND ART\|[0002] The saline-alkali soil has the problems of deterioration of physical and chemical properties of soil, insufficient nutrient supply, limited plant growth and the like due to high salt content and strong alkalinity.\|[0003] The conventional saline-alkali soil improvement methods comprise salt removal, salt pressing, organic fertilizer application, chemical modifier application and the like, but the methods have the defects of slow effect, high cost, high environmental risk or difficult long-term maintenance of improvement effect and the like. In recent years, mineral fertilizers have been greatly developed in the aspect of saline-alkali soil improvement, silicate minerals are utilized for weathering to release nutrient elements such as calcium, magnesium, potassium, phosphorus and the like, carbonate minerals are formed by reaction with atmospheric carbon dioxide, and research on soil improvement, nutrient supplementation, carbon fixation and sink increase is increasingly paid attention to. However, the existing research is still imperfect in simulating leaching and chemical weathering rules of silicate minerals under the conditions of natural precipitation and soil temperature and humidity, and lacks experimental verification and model support of a system. In practical researches, the following problems are common in the conventional silicate mineral chemical weathering leaching experimental device:\| (1) By adopting a manual liquid adding mode, the leaching solution amount is difficult to be matched with the natural precipitation condition; \| (2) Only is carried out at room temperature, lacks heating and temperature control functions, and cannot reflect the change of the real soil under the temperature and humidity conditions. \|[0004] The problems cause great deviation between laboratory simulated silicate mineral weathering experimental results and chemical weathering under actual natural conditions, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain. Therefore, development of a chemical weathering leaching experimental device capable of simulating silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment is needed to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners and novel mineral fertilizers.\|DISCLOSURE\|Disclosure of Invention\|[0005] Based on the problem that the laboratory simulation silicate mineral weathering experimental result in the prior art has larger deviation from the chemical weathering under the actual natural condition, and reliable silicate mineral weathering rate, nutrient release and carbon fixing process data are difficult to obtain, the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions, which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable temperature and humidity conditions, so as to truly simulate the chemical weathering process of silicate minerals in the natural environment of saline-alkali soil, and provide scientific basis and experimental support for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers.\|[0006] In order to achieve the purpose, the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided, and comprises:\| The temperature control device comprises a support frame and an incubator device arranged on the support frame; \| The leaching assembly comprises a leaching column arranged in the incubator device and a liquid collecting container arranged below the leaching column, wherein two axial ends of the leaching column respectively extend out of the incubator device, the top end of the leaching column is in an open shape, and the bottom end of the leaching column is provided with a liquid discharging pipe communicated with the liquid collecting container; \| a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column; \| a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time, a probe of the temperature and humidity sensor being inserted into the leaching column, and \|And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%.\|[0007] Further, the rainfall simulation device comprises a spraying component arranged at the open top of the leaching column, a syringe pump mechanism for drawing and pumping leaching solution, a liquid delivery pipe for connecting the spraying component with a liquid outlet port of the syringe pump mechanism, a water inlet pipe for connecting a liquid inlet port of the syringe pump mechanism with a liquid storage container, and a supporting seat for supporting the syringe pump mechanism, wherein the syringe pump mechanism is fixedly arranged on the supporting seat, the leaching device for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity further comprises a driving device for driving the syringe pump mechanism to draw and pump leaching solution, a first valve arranged at the liquid inlet port of the syringe pump mechanism and a second valve arranged at the liquid outlet port of the syringe pump mechanism, the driving device is arranged on the supporting seat, and the driving device, the first valve and the second valve can be controlled to work and are respectively and electrically connected with the controller.\|[0008] Further, the injection pump mechanism comprises an injection cylinder, a first piston, a second piston, a push-pull rod, a first linkage rod, a sleeve and a second linkage rod, wherein the two ends of the injection cylinder are respectively in an opening shape, the first piston is arranged in the injection cylinder in a sliding mode, the second piston is arranged in the injection cylinder in a sliding mode, the push-pull rod is used for driving the first piston to move along the axial direction of the injection cylinder, the first linkage rod is connected with one end, far away from the first piston, of the push-pull rod, the sleeve is used for driving the second piston to move along the axial direction of the injection cylinder, the second linkage rod is connected with one end, far away from the second piston, of the sleeve, a first sliding hole is formed in the second piston, the outer peripheral surface of the push-pull rod is in interference contact with the inner hole wall of the first sliding hole, the sleeve can be sleeved on the push-pull rod in an axial sliding mode, and the first linkage rod and the second linkage rod are respectively connected with the driving device.\|[0009] Further, the driving device comprises a driving assembly, a connecting rod mechanism connecting the first linkage rod with the second linkage rod, and a gear mechanism connecting the connecting rod mechanism with the driving assembly, wherein the gear mechanism comprises a first gear rotatably installed on the supporting seat and a second gear rotatably installed on the supporting seat, the first gear is meshed with the second gear, the first gear and/or the second gear are/is connected with the driving assembly so that the driving assembly can drive the first gear and the second gear to synchronously rotate, the connecting rod mechanism comprises a first driving rod fixedly connected with the first gear, a first connecting rod rotatably connecting the first end of the first driving rod with the first end of the first linkage rod, a second connecting rod rotatably connecting the second end of the first driving rod with the first end of the second linkage rod, a second driving rod fixedly connected with the second gear, a second connecting rod fixedly connected with the second end of the second driving rod, a second connecting rod fixedly connected with the second end of the second connecting rod, a second connecting rod with the second connecting rod, and a first connecting rod with the second connecting rod, and a second connecting rod with the second connecting rod, and the connecting rod with the second connecting rod with the first connecting rod and the second connecting rod with the second connecting rod.\|[0010] Further, the driving assembly comprises a first driving shaft arranged on the supporting seat in a rotating mode, a second driving shaft arranged on the supporting seat in a rotating mode, a driving motor fixedly installed on the supporting seat, a first synchronous belt wheel fixedly sleeved on the first driving shaft, a second synchronous belt wheel fixedly sleeved on the second driving shaft, a third synchronous belt wheel fixedly sleeved on a motor shaft of the driving motor, and a synchronous belt connecting the first synchronous belt wheel, the second synchronous belt wheel and the third synchronous belt wheel, wherein the driving motor is electrically connected with the controller.\|[0011] Further, a pressure sensor for detecting the leaching solution pressure in the injection cylinder is arranged in the injection cylinder, and the pressure sensor is electrically connected with the controller.\|[0012] Further, the leaching assembly further comprises a first mesh plate arranged in a leaching cavity in the leaching column and a first filter screen paved on the mesh plate, silicate rock powder in the leaching column forms a columnar rock body, and the bottom end of the columnar rock body is supported on the first mesh plate.\|[0013] Further, the incubator device includes the incubator that inside was equipped with the constant temperature chamber, set up in on the incubator in order to open or close selectively the chamber door in constant temperature chamber, set up in inside in order to realize the refrigerator of constant temperature intracavity temperature regulation of incubator, and set up in inside air cycle and the heating mechanism of incubator, air cycle and the heating mechanism can be accelerated air cycle flow in the constant temperature chamber, and heat air in the constant temperature chamber, the controller can be according to humidity and the temperature control that temperature and humidity sensor detected the refrigerator air cycle and the heating mechanism work, adjust the temperature in the constant temperature chamber, so that the temperature in the constant temperature chamber keeps in the preset temperature range of 0 ℃ to 25 ℃.\|[0014] Further, the air circulation and heat supply mechanism comprises a circulation air channel arranged in the constant temperature cavity, an air inlet pipe communicated with an air inlet of the circulation air channel, an air return pipe communicated with an air return port of the circulation air channel, a heating component arranged in the circulation air channel and a circulation fan arranged in the circulation air channel, wherein the heating component comprises a plurality of heating pipes which are transversely arranged.\|[0015] Further, the spraying assembly comprises a spray head connected with the infusion tube and a spraying support for supporting the spray head on the support frame and/or at the top end of the leaching column, and the spraying support is detachably connected with the support frame and/or the leaching column.\|[0016] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:\| According to the leaching equipment for simulating chemical weathering under the natural temperature and humidity conditions of silicate rock powder, which is disclosed by the embodiment of the invention, the actual natural rainfall and the natural saline-alkali soil temperature and humidity conditions can be simulated, and mineral chemical weathering of the precipitation amount is simulated according to the actual temperature and humidity of the saline-alkali soil, so that the chemical weathering process of silicate minerals in the natural environment of the saline-alkali soil is simulated truly, the true accuracy of the silicate mineral chemical weathering experimental result is improved, and the reliable weathering reaction, salt replacement and carbon fixing process data of the silicate minerals in the saline-alkali soil are obtained, so that scientific basis and experimental support are provided for the research and development of multifunctional silicate mineral conditioning agents and novel mineral fertilizers. \|DRAWINGS DESCRIPTION\|[0017] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0018] FIG. 1 is a schematic diagram of a three-dimensional structure of leaching equipment simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions;\| FIG. 2 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 3 is a schematic top view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 4 is another schematic perspective view of a leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention; \| FIG. 5 is an assembly diagram of a rainfall simulation device and a driving device according to an embodiment of the present invention in a first working state; \| FIG. 6 is a schematic cross-sectional view of the structure shown in FIG. 5; \| fig. 7 is an assembly diagram of the rainfall simulation device and the driving device provided by the embodiment of the invention in a second working state; \| FIG. 8 is a schematic top view of the structure shown in FIG. 7; \| FIG. 9 is a schematic cross-sectional view of the structure shown in FIG. 7; \| Fig. 10 is a schematic perspective view of a leaching assembly according to an embodiment of the present invention; \| FIG. 11 is a schematic cross-sectional view of a leaching assembly according to an embodiment of the present invention; \| FIG. 12 is an exploded view of a leaching assembly provided by an embodiment of the present invention; \| FIG. 13 is a schematic perspective view of an incubator assembly according to an embodiment of the present invention; \| Fig. 14 is a schematic cross-sectional structure of an incubator assembly according to an embodiment of the present invention. \|[0019] Wherein, each reference sign in the figure:\| 1-temperature control device, 11-supporting frame, 12-incubator device, 121-incubator, 122-oven door, 123-refrigerator, 124-air circulation and heat supply mechanism, 1241-circulation air duct, 1242-muffler, 1243-heating assembly, 1244-circulation fan, 1245-air inlet pipe, 125-mounting hole and 126-observation window; \| 2-leaching components, 21-leaching columns, 22-liquid collecting containers, 23-liquid discharge pipes, 24-first mesh plates, 25-first filter screens, 26-second filter screens and 27-second mesh plates; \| 3-a rainfall simulation device, 31-a spray assembly, 311-a spray head, 312-a spray bracket, 32-a syringe pump mechanism, 321-a syringe, 322-a first piston, 323-a second piston, 324-a push-pull rod, 325-a first linkage rod, 326-a sleeve, 327-a second linkage rod, 33-a transfusion tube, 34-a water inlet tube and 35-a supporting seat; \| 4-drive means, 41-drive assembly, 411-first drive shaft, 412-second drive shaft, 413-drive motor, 414-first timing pulley, 415-second timing pulley, 416-third timing pulley, 417-timing belt, 418-motor shaft, 42-link mechanism, 421-first drive rod, 422-first link, 423-second link, 424-second drive rod, 425-third link, 426-fourth link, 43-gear mechanism, 431-first gear, 432-second gear; \| 5-fixed support, 6-bolt piece, 7-liquid storage space, 8-columnar rock mass and 9-controller. \|INVENTION MODE\|Detailed Description\|[0020] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0021] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, features defining "first," "second," and "third" may explicitly or implicitly include one or more such features. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0022] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.\|[0023] Referring to fig. 1 to 14, a description will now be given of an leaching apparatus for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions according to an embodiment of the present invention. Referring to fig. 1, fig. 2, fig. 3 and fig. 4 in combination, the leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions provided by the embodiment of the invention comprises a temperature control device 1, a leaching assembly 2, a rainfall simulation device 3, a temperature and humidity sensor and a controller 9, wherein the temperature control device 1 comprises a support frame 11 and a constant temperature box device 12 arranged on the support frame 11. The leaching assembly 2 comprises a leaching column 21 arranged in the incubator device 12 and a liquid collecting container 22 arranged below the leaching column 21, wherein two axial ends of the leaching column 21 respectively extend out of the incubator device 12, the top end of the leaching column 21 is open, and a liquid discharging pipe 23 communicated with the liquid collecting container 22 is arranged at the bottom end of the leaching column 21. Wherein, the leaching column 21 is a column-shaped leaching container made of high-temperature resistant transparent plastic or high-temperature resistant transparent organic glass. The rainfall simulation device 3 is used for simulating rainfall so that the leaching solution can uniformly flow into silicate rock powder in the leaching column 21 through the top end opening of the leaching column 21. The temperature and humidity sensor is used for detecting the temperature and humidity of silicate rock powder in the leaching column 21 in real time, and a probe of the temperature and humidity sensor is inserted into the leaching column 21. It should be noted that, the temperature and humidity sensor is implemented by adopting the prior art, and its working principle and structure are well known to those skilled in the art, and are not described herein. The controller 9 is used for controlling the rainfall simulation device 3 and the incubator device 12 to work according to the humidity and the temperature detected by the temperature and humidity sensor, so that the temperature of the silicate rock powder in the leaching column 21 is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column 21 is maintained at 30-80%. It should be noted that the controller 9 may be, but is not limited to, a programmable logic controller.\|[0024] The basic working principle of the leaching equipment for simulating chemical weathering of silicate rock powder under the natural temperature and humidity condition is that silicate rock is crushed into silicate rock powder with the particle size of 0.1 micron, the silicate rock powder and a certain amount of saline-alkali soil are uniformly mixed and filled in a leaching column 21 of a leaching assembly 2, and a rainfall simulation device 3 is arranged at the opening at the top end of the leaching column 21. The simulated rainfall device 3 carries out real simulated rainfall characteristics on the leaching solution, so that the leaching solution can flow into the silicate rock powder in the leaching column 21 through the opening at the top end of the leaching column 21, the silicate rock powder in the leaching column 21 can be uniformly leached, disturbance on the silicate rock powder in the leaching column 21 is reduced, leaching efficiency and leaching effect of the silicate rock powder in the leaching column 21 are improved, and accuracy of silicate mineral chemical weathering experimental results is improved. In addition, during leaching, the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, and after the leaching solution permeates the silicate rock powder in the leaching column 21, the leaching solution is drained into the liquid collecting container 22 through the liquid drain pipe 23 at the bottom end of the leaching column 21. And, in the whole process of the chemical weathering experiment, the temperature in the incubator device 1 and the humidity in the leaching column 21 are detected in real time through the temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is less than 0 ℃, the controller 9 controls the heating component in the incubator device 1 to heat and work until the temperature in the incubator device 1 reaches 25 ℃, and the controller 9 controls the heating component in the incubator device 1 to stop heating and work. When the temperature in the oven apparatus 1 is greater than 25 ℃, the controller 9 controls the refrigerator in the oven apparatus 1 to operate until the temperature in the oven apparatus 1 reaches 25 ℃, and the controller 9 controls the refrigerator in the oven apparatus 1 to stop the cooling operation. The circulation is such that the temperature in the oven apparatus 1 is controlled within a preset temperature range of 0 to 25 ℃, thereby making the silicate rock powder in the leaching column 21 subjected to the chemical weathering simulation experiment under the temperature condition of 0 to 25 ℃. Of course, the controller 9 may also control the operation of the heating element and/or the refrigerator in the incubator apparatus 1 so that the temperature in the incubator apparatus 1 is stabilized at any one of the preset temperature values between 0 ℃ and 25 ℃ and so that the silicate powder in the leaching column 21 is subjected to chemical weathering simulation test under a specific temperature condition (e.g., 5 ℃, 10 ℃, 15 ℃, 20 ℃,25 ℃ or the like) between 0 ℃ and 25 ℃. Meanwhile, when the humidity in the leaching column 21 is less than 30%, the controller 9 controls the rainfall simulation device 3 to work, so that the rainfall simulation device 3 sprays leaching solution to silicate rock powder in the leaching column 21 uniformly at a certain flow rate, until the humidity in the leaching column 21 reaches 80%, the controller 9 controls the rainfall simulation device 3 to stop working, and the circulation is performed in such a way that the humidity in the leaching column 21 is controlled within a preset humidity range of 30-80%, and thus chemical weathering simulation experiments are performed on the silicate rock powder in the leaching column 21 under a humidity condition of 30-80%. Therefore, the method can simulate the actual natural rainfall and the natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, simulate the mineral chemical weathering of the precipitation according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and improve the true accuracy of the silicate mineral chemical weathering experimental result so as to obtain the reliable weathering reaction, salt replacement and carbon fixation process data of the silicate minerals of the saline-alkali soil, thereby being beneficial to improving the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|[0025] Referring to fig. 2,3 and 4, in some embodiments, the rainfall simulation device 3 includes a spray assembly 31 disposed at an opening at a top end of the leaching column 21, a syringe pump mechanism 32 for drawing and pumping the leaching solution, a transfusion tube 33 connecting the spray assembly 31 and a liquid outlet port of the syringe pump mechanism 32, a water inlet pipe 34 for connecting a liquid inlet port of the syringe pump mechanism 32 with a liquid storage container, and a support seat 35 for supporting the syringe pump mechanism 32, the syringe pump mechanism 32 is fixedly mounted on the support seat 35, the leaching device for simulating chemical weathering of silicate powder under natural temperature and humidity conditions further includes a driving device 4 for driving the syringe pump mechanism 32 to draw and pump the leaching solution, a first valve disposed at the liquid inlet port of the syringe pump mechanism 32 and a second valve disposed at the liquid outlet port of the syringe pump mechanism 32, the driving device 4 is disposed on the support seat 35, and the controller 9 can control the driving device 4, the first valve and the second valve to work, and the driving device 4, the first valve and the second valve are respectively electrically connected with the controller 9. It will be appreciated that in some of these embodiments the first valve 9 and the second valve 10 are solenoid valves. By the above arrangement, the silicate rock is crushed into silicate rock powder having a particle size of 0.1 μm, the silicate rock powder is packed in the leaching column 21 of the leaching assembly 2, and the spraying assembly 31 is installed at the top end opening of the leaching column 21. When the injection pump mechanism 32 is required to be used for sucking the leaching solution from the liquid storage container under the negative pressure, the controller controls the first valve 9 to open the liquid inlet of the injection pump mechanism 32, the controller controls the second valve 10 to close the liquid outlet of the injection pump mechanism 32, the driving device 4 drives the injection pump mechanism 32 to suck the leaching solution from the liquid storage container under the negative pressure, until the leaching solution in the injection pump mechanism 32 is full, the controller controls the first valve 9 to close the liquid inlet of the injection pump mechanism 32, and the controller controls the second valve 10 to open the liquid outlet of the injection pump mechanism 32, the injection pump mechanism 32 can pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the simulated rainfall device 3 under the driving action of the driving device 4, the real rainfall simulation characteristic is realized, the uniformity of the silicate powder in the leaching column 21 is ensured, the silicate powder in the leaching column 21 is uniformly leached, the disturbance of the silicate powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate powder in the leaching column 21 are further improved, and the accuracy of silicate mineral chemical weathering experiment results is facilitated. In addition, during leaching, the leaching solution of the silicate powder in the leaching column 21 is uniformly sprayed to the leaching column 21 at a certain flow rate through the spraying assembly 31, and is drained into the liquid collecting container 22 through the drain pipe 23 at the bottom end of the leaching column 21 after penetrating the silicate powder in the leaching column 21.\|[0026] Therefore, in the leaching device for simulating chemical weathering of silicate rock powder under the natural temperature and humidity conditions, when the controller controls the first valve 9 to be opened and the second valve 10 to be closed, the driving device 4 can drive the injection pump mechanism 32 to draw the leaching solution from the liquid storage container through negative pressure until the injection pump mechanism 32 draws enough leaching solution, then the controller controls the first valve 9 to be closed and the second valve 10 to be opened, the injection pump mechanism 32 can continuously pump the leaching solution in the injection pump mechanism 32 to the spraying assembly 31 of the rainfall simulator 3 under the driving action of the driving device 4, the real rainfall simulation characteristic of the spraying assembly 31 of the rainfall simulator 3 is adopted to ensure the uniformity of the leaching solution flowing into the silicate rock powder in the leaching column 21, so that the silicate rock powder in the leaching column 21 can be uniformly leached, the disturbance of the silicate rock powder in the leaching column 21 is reduced, the leaching efficiency and the leaching effect of the silicate rock powder in the leaching column 21 are improved, and the accuracy of the silicate mineral chemical weathering experiment result is improved.\|[0027] Referring to fig. 2,6 and 9 in combination, in some embodiments, the syringe pump mechanism 32 includes a syringe 321, a first piston 322, a second piston 323, a push-pull rod 324, a first linkage rod 325, a sleeve 326 and a second linkage rod 327, two ends of the syringe 321 are all open, the first piston 322 and the second piston 323 are respectively slidably disposed in the syringe 321, and when the first piston 322 and the second piston 323 are respectively slid to the openings at two ends of the syringe 321, a closed liquid storage space 7 for storing the shower solution can be formed in the syringe 321, and the liquid storage capacity of the liquid storage space 7 can be preset. The push-pull rod 324 is used for driving the first piston 322 to move along the axial direction of the injection cylinder 321, the sleeve 326 is used for driving the second piston 323 to move along the axial direction of the injection cylinder 321, and when the first piston 322 and the second piston 323 move away from each other along the axial direction of the injection cylinder 321, the solution can be pumped from the liquid storage container through the injection pump mechanism 32, and the pumped solution can be stored in the closed liquid storage space 7 between the first piston 322 and the second piston 323. When the first piston 322 and the second piston 323 move closer to each other in the axial direction of the syringe 321, the shower solution in the solution storage space 7 can be continuously pumped to the shower assembly 31 of the rainfall simulation device 3 by the syringe pump mechanism 32. The first linkage rod 325 is connected with one end of the push-pull rod 324 far away from the first piston 322, the second linkage rod 327 is connected with one end of the sleeve 326 far away from the second piston 323, the first linkage rod 325 and the second linkage rod 327 are respectively connected with the driving device 4, a first sliding hole for the push-pull rod 324 to pass through is arranged on the second piston 323, the outer peripheral surface of the push-pull rod 324 is in interference contact with the inner hole wall of the first sliding hole, and the sleeve 326 can be sleeved on the push-pull rod 324 in an axial sliding manner. When the driving device 4 drives the first linkage rod 325 and the second linkage rod 327, the sleeve 326 is sleeved on the push-pull rod 324 in a sliding manner along the axial direction, so that the first piston 322 and the second piston 323 can move towards or away from each other along the axial direction of the injection cylinder 321. It should be noted that, the liquid inlet port and the liquid outlet port are both disposed on the syringe 321, and the liquid inlet port and the liquid outlet port are respectively communicated with the liquid storage space 7.\|[0028] Referring to fig. 4, 5, 7 and 8 in combination, in some embodiments, the driving device 4 includes a driving assembly 41, a link mechanism 42 and a gear mechanism 43, the link mechanism 42 is used to connect the first link lever 325 with the second link lever 327, the gear mechanism 43 is used to connect the link mechanism 42 with the driving assembly 41, the gear mechanism 43 includes a first gear 431 rotatably mounted on the support seat 35 and a second gear 432 rotatably mounted on the support seat 35, the first gear 431 and the second gear 432 are the same in size and structure, the first gear 431 and the second gear 432 mesh, the first gear 431 and the second gear 432 are connected with the driving assembly 41, and one gear of the first gear 431 and the second gear 432 may be connected with the driving assembly 41, so that the driving assembly 41 can drive the first gear 431 and the second gear 432 to rotate synchronously. The link mechanism 42 includes a first driving lever 421 fixedly coupled to a first gear 431, a first link 422 rotatably coupling a first end of the first driving lever 421 with a first end of a first link lever 325, a second link 423 rotatably coupling a second end of the first driving lever 421 with a first end of a second link lever 327, a second driving lever 424 fixedly coupled to a second gear 432, a third link 425 rotatably coupling a first end of the second driving lever 424 with a second end of the first link lever 325, a fourth link 426 rotatably coupling a second end of the second driving lever 424 with a first end of the second link lever 327, the lengths of the first link 422, the second link 423, the third link 425, and the fourth link 426 being equal, the length of the first link lever 325 being equal to the length of the second link lever 327, and the length of the first driving lever 421 being equal to the length of the second link lever 424. It should be noted that, two ends of the first link 422 are respectively rotatably connected to the first end of the first driving rod 421 and the first end of the first linkage rod 325 through a pivot, and two ends of the second link 423 are respectively rotatably connected to the second end of the first driving rod 421 and the second end of the first linkage rod 325 through a pivot. Through the above structure, the driving assembly 41 can synchronously drive the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321, and can improve the stability of the first piston 322 and the second piston 323 to move close to or away from each other along the axial direction of the injection cylinder 321. In addition, the connecting rod mechanism 42 is driven by the rotation of the gear mechanism 43 to drive the first piston 322 and the second piston 323 to move close to each other along the axial direction of the injection cylinder 321, and the speed of the injection pump mechanism 32 for pumping the leaching solution can be controlled by controlling the rotation speed of the first gear 431 and/or the second gear 432, so that the leaching rate can be controlled and regulated according to the leaching experiment requirement.\|[0029] Referring to fig. 4, 5 and 7, in some embodiments, the driving assembly 41 includes a first driving shaft 411, a second driving shaft 412, a driving motor 413, a first synchronous belt 417 wheel 414, a second synchronous belt 417 wheel 415, a third synchronous belt 417 wheel 416 and a synchronous belt 417, the first driving shaft 411 and the second driving shaft 412 are respectively rotatably disposed on the supporting seat 35, the driving motor 413 is fixedly mounted on the supporting seat 35, the first synchronous belt 417 wheel 414 is fixedly sleeved on the first driving shaft 411, the second synchronous belt 417 wheel 415 is fixedly sleeved on the second driving shaft 412, the third synchronous belt 417 wheel 416 is fixedly sleeved on a motor shaft 418 of the driving motor 413, and the synchronous belt 417 connects the first synchronous belt 417 wheel 414, the second synchronous belt 417 wheel 415 and the third synchronous belt 417 wheel 416, and the driving motor 413 is electrically connected with the controller. Through the above structure arrangement, under the driving action of the driving motor 413, the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 synchronously rotate, so as to drive the gear mechanism 43 to rotate, and the gear mechanism 43 drives the first piston 322 and the second piston 323 to move close to or far away from each other along the axial direction of the injection cylinder 321 through the link mechanism 42, so that the injection pump mechanism 32 can finish the action of drawing and pumping the shower solution.\|[0030] Referring to fig. 2, 4 and 5, in some embodiments, the first gear 431 is fixedly sleeved on the first driving shaft 411, the second gear 432 is fixedly sleeved on the second driving shaft 412, and the first driving shaft 411, the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are arranged in an isosceles triangle, so that the distance between the first driving shaft 411 and the second driving shaft 412, the distance between the first driving shaft 411 and the motor shaft 418 of the driving motor 413, and the distance between the second driving shaft 412 and the motor shaft 418 of the driving motor 413 are all equal. By the above arrangement, the stability of the movement of the first piston 322 and the second piston 323 in the axial direction of the syringe 321 toward each other or away from each other can be improved.\|[0031] In some embodiments, a pressure sensor for detecting leaching liquid pressure inside the syringe 321 is disposed in the syringe 321, and the pressure sensor is electrically connected to the controller. The controller can control the rotation speed of the driving motor 413 to control the rotation speed of the first gear 431 and/or the second gear 432 according to the pressure detected by the pressure sensor, so as to control the speed of the injection pump mechanism 32 for pumping the leaching solution, thereby being convenient for controlling and adjusting the leaching rate according to the leaching experiment requirement.\|[0032] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a first mesh plate 24 disposed in the leaching chamber in the leaching column 21 and a first filter screen 25 laid on the mesh plate, silicate rock powder in the leaching column 21 forms a columnar rock body 8, and a bottom end of the columnar rock body 8 is supported on the first mesh plate 24. Through the structure setting, through adopting the first mesh board 24 that plastics or metal etc. made to the silicate rock powder in the leaching column 21 to form column rock mass 8 bottom formation support, the leaching solution after the rethread first filter screen 25 on the first mesh board 24 filters, can prevent effectively that the silicate rock powder in the leaching column 21 from forming column rock mass 8 bottom and collapsing, ensure simultaneously that the leaching solution that liquid collecting container 22 collected does not contain silicate rock powder, be favorable to improving the accuracy of leaching experiment. The mesh size of the first screen 25 is smaller than the particle size of the silicate powder.\|[0033] Referring to fig. 10, 11 and 12 in combination, in some embodiments, the leaching assembly 2 further includes a second screen 26 disposed on top of the columnar rock mass 8 and a second mesh plate 27 disposed over the second screen 26. By paving the second filter screen 26 on the top end of the columnar rock body 8 formed by silicate rock powder in the leaching column 21 and covering the second filter screen 26 with a second mesh plate 27 made of hard materials such as plastics or metals, the integrity of the top of the columnar rock body 8 is prevented from being damaged due to the fact that the concentrated impact of leaching solution water flows form a dent.\|[0034] Referring to fig. 2 and 4 in combination, in some embodiments, spray assembly 31 includes a spray head 311 coupled to a fluid line 33, and a spray bracket 312 for supporting spray head 311 on support frame 1 and/or on the top of leaching column 21, spray bracket 312 being removably coupled to support frame 1 and/or leaching column 21. It should be noted that the spray head 311 may be, but is not limited to, an atomizing spray head 311. In actual operation, the speed of the driving motor 413 is controlled, and various rainfall is simulated by adopting the atomizing nozzle 311, so that silicate rock powder in the leaching column 21 forms a columnar rock body 8, and the problems that the soil column structure is damaged and the leaching speed of water is influenced due to the fact that water flow impacts to form a recess are avoided.\|[0035] Referring to fig. 13 and 14 in combination, in some embodiments, the incubator apparatus 12 includes an incubator 121 having a constant temperature chamber therein, a door 122 provided on the incubator 121 to selectively open or close the constant temperature chamber, a refrigerator 123 provided inside the incubator 121 to achieve temperature adjustment in the constant temperature chamber, and an air circulation and heat supply mechanism 124 provided inside the incubator 121, the air circulation and heat supply mechanism 124 being capable of accelerating the air circulation flow in the constant temperature chamber and heating the air in the constant temperature chamber, and the controller 9 being capable of controlling the operation of the refrigerator 123, the air circulation and heat supply mechanism 124 according to the humidity and temperature detected by the temperature and humidity sensor to adjust the temperature in the constant temperature chamber so as to maintain the temperature in the constant temperature chamber within a preset temperature range of 0 to 25 ℃ or to any specific temperature value between 0 to 25 ℃. The incubator 121 is provided with a mounting hole 125 for accommodating and mounting the leaching column 21, and the outer side wall of the leaching column 21 is in airtight contact with the inner hole wall of the mounting hole 125. The door 122 is provided with a transparent observation window 126 made of high temperature resistant glass so as to observe leaching conditions in the leaching column 21 inside the incubator 121. In the whole process of chemical weathering experiment, the temperature in the incubator device 1 is detected in real time through a temperature and humidity sensor, the temperature and humidity sensor feeds back the detected temperature and humidity to the controller 9, when the temperature in the incubator device 1 is smaller than 0 ℃, the controller 9 controls the refrigerator 123 to be closed and controls the air circulation and heat supply mechanism 124 in the heat preservation 121 to work, and the air circulation and heat supply mechanism 124 accelerates the air circulation flow in the constant temperature cavity and heats the air in the constant temperature cavity, so that the temperature in the constant temperature cavity of the incubator 121 is quickly increased until the temperature in the constant temperature cavity of the incubator 121 reaches 25 ℃, and the controller 9 controls the air circulation and heat supply mechanism 124 in the incubator device 1 to stop heating work. If the temperature in the constant temperature chamber of the incubator 121 is higher than 25 ℃, the controller 9 controls the refrigerator 123 to operate and controls the air circulation and heating mechanism 124 to stop operating, so that the temperature in the constant temperature chamber is reduced by between 0 and 25 ℃. By means of the circulation, the temperature in the heat preservation box 121 can be controlled within a preset temperature range of 0-25 ℃, so that silicate rock powder in the leaching column 21 is subjected to chemical weathering simulation experiments under the temperature condition of 0-25 ℃ to simulate actual natural rainfall and natural temperature and humidity conditions of the soil surface of the natural saline-alkali soil, mineral chemical weathering of simulated precipitation is performed according to the actual temperature and humidity of the soil surface of the saline-alkali soil, and the actual accuracy of silicate mineral chemical weathering experiment results is improved.\|[0036] Referring to fig. 13 and 14 in combination, in some embodiments, the air circulation and heat supply mechanism 124 includes a circulation duct 1241 disposed in the constant temperature chamber, an air inlet pipe 1245 connected to an air inlet of the circulation duct 1241, an air return pipe 1242 connected to an air return port of the circulation duct 1241, a heating assembly 1243 disposed in the circulation duct 1241, and a circulation fan 1244 disposed in the circulation duct 1241, the heating assembly 1243 including a plurality of heating pipes disposed transversely. When the air circulation and heat supply mechanism 124 works, air in the constant temperature cavity is led into the circulation air channel 1241 by the air inlet pipe 1245 under the action of the circulation fan 45, the air in the circulation air channel 1241 is heated by the heating component 1244 and then becomes hot air, and the hot air in the circulation air channel 1241 flows back to the constant temperature cavity by the air return pipe 1243, so that the air circulation and heat supply mechanism 124 can be used for quickly heating the air in the constant temperature cavity.\|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.	Family Number\|(117662153)\|117662153\|Object of Invention\|(CN121454002 A)\|In order to achieve the purpose , the invention adopts the technical scheme that the leaching equipment for simulating chemical weathering of silicate rock powder under the condition of natural temperature and humidity is provided , and comprises : \|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions , and belongs to the technical fields of enhanced rock weathering carbon fixation , mineral fertilizer development and saline soil improvement and management . \|Abstract\|(CN121454002 A)\|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions , and belongs to the technical fields of rock weathering and carbon sequestration enhancement , mineral fertilizer development and saline soil improvement and treatment . The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions . The leaching equipment comprises a temperature control device , a leaching assembly , a rainfall simulation device , a temperature and humidity sensor and a controller , wherein the temperature control device comprises a support frame and a constant temperature box device arranged on the support frame . The leaching assembly comprises a leaching column arranged in the constant - temperature box device and a liquid collecting container arranged below the leaching column . The equipment can simulate a chemical weathering leaching experiment of silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment so as to really simulate a chemical weathering process of the silicate minerals in a natural environment of saline - alkali soil ; scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners , novel mineral fertilizers and saline - alkali soil improvement . \|Title\|(CN121454002 A)\|Leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions \|Advantages / Prev. Drawbacks\|(CN121454002 A)\|( . . . ) actual natural condition , and reliable silicate mineral weathering rate , nutrient release and carbon fixing process data are difficult to obtain , the embodiment of the invention aims to provide the leaching equipment for simulating the chemical weathering of silicate rock powder under the natural temperature and humidity conditions , which can simulate the chemical weathering leaching experiment of silicate minerals under the natural rainfall and soil temperature and humidity conditions under the controllable ( . . . ) \|Independent Claims\|(CN121454002 A)\|1. An leaching device for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions , comprising : ( . . . ) a rainfall simulation device for simulating rainfall so that leaching solution can uniformly flow into silicate rock powder in the leaching column ; a temperature and humidity sensor for detecting the temperature and humidity of silicate rock powder in the leaching column in real time , a probe of the temperature and humidity sensor being inserted into the leaching column , and And the controller is used for controlling the rainfall simulation device and the incubator device to work according to the humidity and the temperature detected by the temperature and humidity sensor , so that the temperature of silicate rock powder in the leaching column is maintained at 0-25 ℃, and the relative humidity of the silicate rock powder in the leaching column is maintained at 30-80%. \|	Analysis of biological materials	G01N-033/00\|G01N-033/00/98\|G01N-033/24		G01N-033/00\|G01N-033/00/98\|G01N-033/24	G01N-033/00\|G01N-033/24	G01N-033/00\|G01N-033/24										PENDING	(CN121454002)\|PENDING	ALIVE	(CN121454002)\|ALIVE	(CN121454002)\|LEGAL DETAILS FOR CN121454002\|Actual or expected expiration date=2045-11-20\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-11-20\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202511707827\|Application date=2025-11-20\|Standardized application number=2025CN-1707827\|Event publication date=2026-02-03\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN121454002\|Publication stage code=A\|Publication date=2026-02-03\|Standardized publication number=CN121454002\|Event publication date=2026-02-03\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2026-02-24\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN121454002)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKc0O21wABuVOlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080718408&ekey=2075&xpn=CN121454002&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=G2LF5CjifuL%252Fkpe3oMQTWZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN121454002)\|CN	(CN121454002)\|NAME=LANZHOU UNIVERSITY , COUNTRY=CN		(CN121454002)\|NAME=HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=41028	(CN121454002)\|CN	(CN121454002)\|NAME=ZHANG JIETANG, COUNTRY=CN \|NAME=LI XINGYUAN\|NAME=GOU XIAOHUA	(CN121454002)\|14	1	1					(CN121454002)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2026-02-03\|Gazette number: GAZNUM=42-0601\|Number of Pages: NPAGES=23\|		(CN121454002)\|CHINESE (CHI)	(CN121454002)\|Patent	Titre: (CN121454002)\|Leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions Résumé: (CN121454002)\|The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions, and belongs to the technical fields of rock weathering and carbon sequestration enhancement, mineral fertilizer development and saline soil improvement and treatment. The invention provides leaching equipment for simulating chemical weathering of silicate rock powder under natural temperature and humidity conditions. The leaching equipment comprises a temperature control device, a leaching assembly, a rainfall simulation device, a temperature and humidity sensor and a controller, wherein the temperature control device comprises a support frame and a constant temperature box device arranged on the support frame. The leaching assembly comprises a leaching column arranged in the constant-temperature box device and a liquid collecting container arranged below the leaching column. The equipment can simulate a chemical weathering leaching experiment of silicate minerals under the conditions of natural rainfall and soil temperature and humidity in a controllable temperature and humidity environment so as to really simulate a chemical weathering process of the silicate minerals in a natural environment of saline-alkali soil; scientific basis and experimental support are provided for research and development of multifunctional silicate mineral conditioners, novel mineral fertilizers and saline-alkali soil improvement.	4	Abstract	gpt-4o-mini	yes	The article describes leaching equipment designed to simulate chemical weathering of silicate rocks, which is directly related to enhanced weathering and carbon sequestration.
2	US63/213,398\|US63/213,398P\|US63/289,395\|US63/289,395P\|EP22829238\|US17/846,838\|US63/322,672\|US63/322,672P\|WOUS2022/034546\|US18/128,583\|US18/435,492\|US19/335,929	US19/335,929\|US18/435,492\|HK42023083673\|US18/128,583\|WOUS2022/034546\|HK62023083672\|BR112023023226\|EP22829238\|EP23199092\|AU2022299180\|CA3207124\|US17/846,838	US20260016458\|BR112023023226\|EP4256520\|EP4256520\|US12422425\|EP4256520\|AU2022299180\|US20240264139\|EP4276752\|US11921098\|BR112023023226\|HK40094979\|HK40095252\|EP4276752\|BR112023023226\|EP4256520\|US20230273174\|AU2022299180\|US11644454\|CA3207124\|WO2022/271842\|US20220404329	103013820	US20260016458 A1 2026-01-15 [US20260016458]\|US12422425 B2 2025-09-23 [US12422425]\|US20240264139 A1 2024-08-08 [US20240264139]\|HK40094979 A 2024-01-26 [HK40094979]\|US11921098 B2 2024-03-05 [US11921098]\|US20230273174 A1 2023-08-31 [US20230273174]\|WO2022/271842 A1 2022-12-29 [WO2022271842]\|HK40095252 A 2024-01-26 [HK40095252]\|BR112023023226 B1 2026-01-13 [BR112023023226]\|BR112023023226 A2 2024-01-30 [BR112023023226]\|BR112023023226 A0 2023-11-14 [BR112023023226]\|EP4256520 B1 2025-12-10 [EP4256520]\|EP4256520 C0 2025-12-10 [EP4256520]\|EP4256520 A4 2024-11-06 [EP4256520]\|EP4256520 A1 2023-10-11 [EP4256520]\|EP4276752 A3 2024-07-17 [EP4276752]\|EP4276752 A2 2023-11-15 [EP4276752]\|AU2022299180 A9 2024-10-24 [AU2022299180]\|AU2022299180 A1 2023-07-13 [AU2022299180]\|CA3207124 A1 2022-12-29 [CA3207124]\|US11644454 B2 2023-05-09 [US11644454]\|US20220404329 A1 2022-12-22 [US20220404329]	2021-06-22\|2021-12-14\|2022-03-23\|2022-06-22\|2023-03-30\|2024-02-07\|2025-09-22	2025-09-22\|2024-02-07\|2023-12-05\|2023-03-30\|2022-06-22\|2023-12-05\|2022-06-22\|2022-06-22\|2022-06-22\|2022-06-22\|2022-06-22\|2022-06-22	2026-01-15\|2026-01-13\|2025-12-10\|2025-12-10\|2025-09-23\|2024-11-06\|2024-10-24\|2024-08-08\|2024-07-17\|2024-03-05\|2024-01-30\|2024-01-26\|2024-01-26\|2023-11-15\|2023-11-14\|2023-10-11\|2023-08-31\|2023-07-13\|2023-05-09\|2022-12-29\|2022-12-29\|2022-12-22	(EP4256520)\|2025-12-10\|\|(US12422425)\|2025-09-23\|(US11921098)\|2024-03-05\|(US11644454)\|2023-05-09\|\|\|(BR112023023226)\|2026-01-13\|\|\|\|	(EP4256520)\|2042-06-22\|(EP4276752)\|2042-06-22\|(US12422425)\|2042-06-22\|(US11921098)\|2042-06-22\|(US11644454)\|2042-06-22\|(US20260016458)\|2042-06-22\|(WO2022/271842)\|2024-12-22\|(BR112023023226)\|2042-06-22\|(AU2022299180)\|2042-06-22\|(HK40095252)\|2042-06-22\|(HK40094979)\|2043-12-05\|(CA3207124)\|2042-06-22	(EP4256520)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering	(EP4256520)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.	EION	(EP4256520)\|Eion Corp.\|(EP4256520)\|Eion Corp. ([US])\|(EP4256520)\|Eion Corp.\|(EP4256520)\|Eion Corp. ([US])\|(EP4276752)\|Eion Corp. ([US])\|(EP4276752)\|Eion Corp. ([US])\|(US12422425)\|Eion Corp. ([US])\|(US20240264139)\|Eion Corp. ([US])\|(US11921098)\|Eion Corp. ([US])\|(US20230273174)\|Eion Corp. ([US])\|(US11644454)\|Eion Corp. ([US])\|(US20220404329)\|Eion Corp. ([US])\|(US20260016458)\|Eion Corp. ([US])\|(WO2022/271842)\|EION CORP. ([US])\|(BR112023023226)\|CORP EION ([US])\|(BR112023023226)\|CORP EION ([US])\|\|(AU2022299180)\|EION CORP.\|(AU2022299180)\|EION CORP.\|(HK40095252)\|Eion Corp ([US])\|(HK40094979)\|Eion Corp ([US])\|(CA3207124)\|EION CORP. ([US])	WOLF ADAM\|CHANG ELLIOT SUK-HYUN\|TANK ALAN ROBERT	(EP4256520)\|WOLF, Adam\|CHANG, Elliot Suk-Hyun\|TANK, Alan Robert\|(EP4256520)\|WOLF, Adam\|CHANG, Elliot Suk-Hyun\|TANK, Alan Robert\|(EP4256520)\|WOLF, Adam\|CHANG, Elliot Suk-Hyun\|TANK, Alan Robert\|(EP4256520)\|WOLF, Adam\|CHANG, Elliot Suk-Hyun\|TANK, Alan Robert	(EP4256520)\|Dragotti & Associati S.P.A. ([IT])\|Reg. Nb: 101869514\|(EP4276752)\|Dragotti & Associati S.R.L. ([IT])\|Reg. Nb: 101869514\|(US12422425)\|Frost Brown Todd LLP\|VanDrake, III Vance V.\|Johnson Alexander J.\|(US11921098)\|Frost Brown Todd LLP\|VanDrake, III Vance V.\|Johnson Alexander J.\|(US11644454)\|Ulmer & Berne LLP\|Van Drake, III Vance V.\|Johnson Alexander J.\|(WO2022/271842)\|FALK, Daniel T. et al. ([US])\|(AU2022299180)\|AJ Pietras IP Limited ([NZ])\|(HK40095252)\|HNC INNOVATION LIMITED ([HK])\|(HK40094979)\|HNC INNOVATION LIMITED ([HK])\|(CA3207124)\|BURNET, DUCKWORTH & PALMER LLP ([CA])	(EP4256520)\|This is a contrast with measurement schemes for soil organic carbon, in which the landowner or other interested party has an information advantage in terms of where or when to sample, which could be used to achieve a particular carbon measurement objective (high or low).\|VM2 may have an advantage over VM1 in not requiring tracking of a specific location for recovering the sampling column.\|Verification methodology 1 has the advantage that it can provide a direct measure of carbon flux and employs a measurement technique that is mature.\|The potential for ERW as a commercial enterprise is limited by some fundamental issues:\|	(EP4256520)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring the immobile trace elements in a soil sample after application of the mineral amendment to verify application of the mineral amendment, characterized in that the method comprises the steps of: determining the amount of the mineral amendment added to the soil sample, determining the amount of measured divalent cations in the soil sample, determining the fractional carbon dioxide removal by comparing the applied divalent cations to the measured divalent cations in the soil sample.\|	(EP4276752)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|	(EP4276752)\|ENHANCED ROCK(100,2)\|MINERAL AMENDMENT(100,2)\|REMOVING CARBON(100,1)\|VERIFICATION(100,1)\|ENHANCED ROCK WEATHERING(82,1)\|IMMOBILE TRACE ELEMENT(35,1)\|\|(EP4276752)\|ENHANCED ROCK(100,2)\|MINERAL AMENDMENT(100,2)\|REMOVING CARBON(100,1)\|VERIFICATION(100,1)\|ENHANCED ROCK WEATHERING(82,1)\|IMMOBILE TRACE ELEMENT(35,1)\|\|(US12422425)\|MINERAL AMENDMENT(100,22)\|VERIFICATION(100,17)\|REMOVING CARBON(100,12)\|ENHANCED ROCK(100,8)\|COMMINUTED SILICATE MINERAL(68,3)\|SILICATE MINERAL AGGLOMERATION(52,2)\|ENHANCED ROCK WEATHERING(46,2)\|INTERESTED PARTY(45,1)\|RECOVERING SAMPLING COLUMN(38,1)\|FUNDAMENTAL ISSUE(37,1)\|CARBON MEASUREMENT OBJECTIVE(25,1)\|LANDOWNER(23,1)\|SLOW RELEASE ACIDIFIER(22,3)\|IMMOBILE TRACE ELEMENT(21,25)\|COMMERCIAL ENTERPRISE(17,1)\|GIBBSITE(15,2)\|BINDER(14,3)\|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)\|NEODYMIUM(12,11)\|BRUKER PROPRIETARY GEO CALIBRATION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|LANTHANUM(11,9)\|SAMARIUM(11,8)\|SCANDIUM(11,8)\|YTTERBIUM(11,8)\|GADOLINIUM(11,7)\|PRASEODYMIUM(11,6)\|BERYLLIUM(11,2)\|GERMANIUM(11,2)\|RUBIDIUM(11,2)\|ZIRCONIUM(11,2)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|DRAWDOWN CALCULATION(10,4)\|ANDTHE TRANSITION METAL(10,1)\|AVERAGE PARTICLE SIZE(9,4)\|ERW(9,4)\|BLAST FURNACE SLAG(9,2)\|CESIUM(9,2)\|CHROMIUM(9,2)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|RIGOROUS QUANTIFICATION(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|BIOLOGICAL DERIVED COMPONENT(9,1)\|PELLETIZED MINERAL AMENDMENT(9,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|GYPSUM(8,3)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|NONLIMITING CANDIDATE(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|NEGATIVELY CHARGED BICARBONATE HCO(8,1)\|STERILIZED SOIL BEAKER(8,1)\|TRANSITION METAL(7,5)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|DISSOLUTION KINETICS(7,2)\|PHOSPHATE FERTILIZER(7,2)\|PULVERIZED SILICATE(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|CARBON FLUX(6,3)\|CHARGE IMBALANCE(6,2)\|INORGANIC ADDITIVE(6,2)\|MG PPM DETECTION(6,2)\|NEUTRAL GROUND(6,2)\|ROCK PARTICLE(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|AGGREGATED PELLET(6,1)\|AGLIME SUBSTITUTE(6,1)\|AGRICULTURAL SOILS(6,1)\|AGRONOMIC PERFORMANCE EXPECTATION(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|BIOFILM MEDIATING(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|DDIC DTA ESTIMATE(6,1)\|FORSTERITE METRIC TON(6,1)\|FORSTERITE TENDENCY(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INFERRED ION FLUX(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|INTENSE SCRUTINY(6,1)\|MARKETING COLLATERAL(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|NONPROFIT ORGANIZATION(6,1)\|OCEAN ACIDIFICATION(6,1)\|PELLET AGGLOMERATION(6,1)\|PHOSPHORUS ECOSYSTEM LOSS(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|PREAPPLICATION SOIL(6,1)\|PROTONATED MICROBE(6,1)\|PULVERIZED LIMESTONE(6,1)\|RENOWNED CHEMIST(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|REWET BIOMASS(6,1)\|RIGOROUS COMPLIANCE(6,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)\|SOIL CULTIVATED ZONE(6,1)\|SOIL GEOCHEMISTRY(6,1)\|SOIL HYDROLOGY(6,1)\|NACL SOLUTION(5,4)\|PROMETHIUM(5,4)\|PULVERIZATION(5,4)\|TRIPLICATE(5,4)\|CENTRIFUGE CELL(5,3)\|GROWING PLANT(5,2)\|AEROSOL SIZED PARTICLE(5,1)\|AGGREGATING GROUND MINERAL(5,1)\|ANALYTICAL LABORATORY(5,1)\|ANCIENT ROCK FORMATION(5,1)\|ANION CONSERVATION(5,1)\|CATEGORY REGULATION(5,1)\|CATION CONSERVATION(5,1)\|CLAUSE XII(5,1)\|DISSOLVE ALGINATE(5,1)\|DISSOLVED ALGINATE POWDER(5,1)\|DOWNSTREAM ECOSYSTEM(5,1)\|DOWNSTREAM WATERWAY(5,1)\|DTA DH INVERSE(5,1)\|DUST PREVALENCE(5,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)\|FUNGAL ADJUVANT(5,1)\|GROUND MINERAL AGGREGATION(5,1)\|KEY INSIGHT(5,1)\|MICROBIAL CATION EXCHANGER(5,1)\|MINERAL ADJUVANT(5,1)\|MINERAL TON HECTARE(5,1)\|NUTRIENT AVAILABILITY(5,1)\|PELLET DISSOLUTION(5,1)\|PHOSPHATE ZINC PRECIPITATE(5,1)\|PROGRESS FRACTIONATION(5,1)\|QUASI GOVERNMENTAL REGULATOR(5,1)\|RESERVOIR GEOLOGY(5,1)\|SOIL STERILIZATION(5,1)\|SPECIALIZED TOOL(5,1)\|STEAM STERILIZATION(5,1)\|TECHNO ECONOMIC MODELING(5,1)\|ULTIMATE PRICE(5,1)\|UREY REACTION BASIC PREMISE(5,1)\|V MONTE CARLO SIMULATION(5,1)\|VERIFICATION VERSION(5,1)\|VERIFIED ENHANCED ROCK(5,1)\|VOLUNTARY MARKET(5,1)\|RARE EARTH ELEMENT(4,18)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DISSOLUTION ENHANCING(4,1)\|DIVALENT MG(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|LB BROTH(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|PULVERIZED MG(4,1)\|REACTION THERMODYNAMICS(4,1)\|SECURITIZED CARBON REMOVAL(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|UNSEALING SAMPLE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|XRF ANALYSIS(4,1)\|K2H(3,4)\|BAG(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|T N(2,9)\|ANALYTICAL CHEMISTRY(2,3)\|K1H(2,3)\|LYSE(2,3)\|SOIL SAMPLE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|COMPUTING V(2,1)\|CONFIDENCE(2,1)\|CREATED VOID SPACE(2,1)\|DCREMAIN(2,1)\|\|(US20240264139)\|MINERAL AMENDMENT(100,22)\|VERIFICATION(100,17)\|REMOVING CARBON(100,12)\|ENHANCED ROCK(100,8)\|COMMINUTED SILICATE MINERAL(68,3)\|SILICATE MINERAL AGGLOMERATION(57,3)\|ENHANCED ROCK WEATHERING(46,2)\|INTERESTED PARTY(45,1)\|RECOVERING SAMPLING COLUMN(38,1)\|FUNDAMENTAL ISSUE(37,1)\|MINERAL TRANSFORMATION(31,2)\|CARBON MEASUREMENT OBJECTIVE(25,1)\|LANDOWNER(23,1)\|SLOW RELEASE ACIDIFIER(22,3)\|IMMOBILE TRACE ELEMENT(21,25)\|COMMERCIAL ENTERPRISE(17,1)\|GIBBSITE(15,2)\|BINDER(14,3)\|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)\|NEODYMIUM(12,11)\|BRUKER PROPRIETARY GEO CALIBRATION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|LANTHANUM(11,9)\|SAMARIUM(11,8)\|SCANDIUM(11,8)\|YTTERBIUM(11,8)\|GADOLINIUM(11,7)\|PRASEODYMIUM(11,6)\|BERYLLIUM(11,2)\|GERMANIUM(11,2)\|RUBIDIUM(11,2)\|ZIRCONIUM(11,2)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|DRAWDOWN CALCULATION(10,4)\|VROCK MONTE CARLO SIMULATION(10,1)\|AVERAGE PARTICLE SIZE(9,4)\|ERW(9,4)\|BLAST FURNACE SLAG(9,2)\|CASO(9,2)\|CESIUM(9,2)\|CHROMIUM(9,2)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|RIGOROUS QUANTIFICATION(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|BIOLOGICAL DERIVED COMPONENT(9,1)\|PELLETIZED MINERAL AMENDMENT(9,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|GYPSUM(8,3)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|NONLIMITING CANDIDATE(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|STERILIZED SOIL BEAKER(8,1)\|TRANSITION METAL(7,5)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|COMPUTING VROCK(7,2)\|DISSOLUTION KINETICS(7,2)\|PHOSPHATE FERTILIZER(7,2)\|PULVERIZED SILICATE(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|CARBON FLUX(6,3)\|CHARGE IMBALANCE(6,2)\|INORGANIC ADDITIVE(6,2)\|MG PPM DETECTION(6,2)\|NEUTRAL GROUND(6,2)\|ROCK PARTICLE(6,2)\|VROCK DOT PRODUCT(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|AGGREGATED PELLET(6,1)\|AGLIME SUBSTITUTE(6,1)\|AGRICULTURAL SOILS(6,1)\|AGRONOMIC PERFORMANCE EXPECTATION(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|BIOFILM MEDIATING(6,1)\|CO2 REAGENT AVAILABILITY(6,1)\|CO2 UPTAKE(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|DDIC DTA ESTIMATE(6,1)\|FORSTERITE METRIC TON(6,1)\|FORSTERITE TENDENCY(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INFERRED ION FLUX(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|INTENSE SCRUTINY(6,1)\|MARKETING COLLATERAL(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|NONPROFIT ORGANIZATION(6,1)\|OCEAN ACIDIFICATION(6,1)\|PELLET AGGLOMERATION(6,1)\|PHOSPHORUS ECOSYSTEM LOSS(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|PREAPPLICATION SOIL(6,1)\|PROTONATED MICROBE(6,1)\|PULVERIZED LIMESTONE(6,1)\|PULVERIZED MG2SIO(6,1)\|RENOWNED CHEMIST(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|REWET BIOMASS(6,1)\|RIGOROUS COMPLIANCE(6,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)\|SOIL CULTIVATED ZONE(6,1)\|SOIL GEOCHEMISTRY(6,1)\|SOIL HYDROLOGY(6,1)\|NACL SOLUTION(5,4)\|PROMETHIUM(5,4)\|PULVERIZATION(5,4)\|TRIPLICATE(5,4)\|CENTRIFUGE CELL(5,3)\|BICARBONATE HCO3(5,2)\|GROWING PLANT(5,2)\|AEROSOL SIZED PARTICLE(5,1)\|AGGREGATING GROUND MINERAL(5,1)\|ANALYTICAL LABORATORY(5,1)\|ANCIENT ROCK FORMATION(5,1)\|ANION CONSERVATION(5,1)\|CATEGORY REGULATION(5,1)\|CATION CONSERVATION(5,1)\|CLAUSE XII(5,1)\|DIFFERENCE VROCK VECTOR(5,1)\|DIFFERENCE VSOIL VECTOR(5,1)\|DISSOLVE ALGINATE(5,1)\|DISSOLVED ALGINATE POWDER(5,1)\|DOWNSTREAM ECOSYSTEM(5,1)\|DOWNSTREAM WATERWAY(5,1)\|DTA DH INVERSE(5,1)\|DUST PREVALENCE(5,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)\|FUNGAL ADJUVANT(5,1)\|GROUND MINERAL AGGREGATION(5,1)\|KEY INSIGHT(5,1)\|MICROBIAL CATION EXCHANGER(5,1)\|MINERAL ADJUVANT(5,1)\|MINERAL TON HECTARE(5,1)\|NUTRIENT AVAILABILITY(5,1)\|PELLET DISSOLUTION(5,1)\|PHOSPHATE ZINC PRECIPITATE(5,1)\|PROGRESS FRACTIONATION(5,1)\|QUASI GOVERNMENTAL REGULATOR(5,1)\|RESERVOIR GEOLOGY(5,1)\|SOIL STERILIZATION(5,1)\|SPECIALIZED TOOL(5,1)\|STEAM STERILIZATION(5,1)\|TECHNO ECONOMIC MODELING(5,1)\|ULTIMATE PRICE(5,1)\|UREY REACTION BASIC PREMISE(5,1)\|VERIFICATION VERSION(5,1)\|VERIFIED ENHANCED ROCK(5,1)\|VOLUNTARY MARKET(5,1)\|RARE EARTH ELEMENT(4,18)\|AQUEOUS CO2(4,2)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DISSOLUTION ENHANCING(4,1)\|DIVALENT MG(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|H2CO SUM(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|LB BROTH(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|REACTION THERMODYNAMICS(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|UNSEALING SAMPLE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|XRF ANALYSIS(4,1)\|BAG(3,2)\|CO2 REMOVAL(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MG MINERAL(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|SOIL SAMPLE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|CO2 MOLECULAR MASS(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|\|(US11921098)\|MINERAL AMENDMENT(100,22)\|VERIFICATION(100,18)\|REMOVING CARBON(100,13)\|ENHANCED ROCK(100,9)\|SILICATE MINERAL AGGLOMERATION(66,2)\|COMMINUTED SILICATE MINERAL(57,3)\|ENHANCED ROCK WEATHERING(46,2)\|INTERESTED PARTY(45,1)\|RECOVERING SAMPLING COLUMN(38,1)\|FUNDAMENTAL ISSUE(37,1)\|MINERAL TRANSFORMATION(31,2)\|CARBON MEASUREMENT OBJECTIVE(25,1)\|LANDOWNER(23,1)\|SLOW RELEASE ACIDIFIER(22,3)\|IMMOBILE TRACE ELEMENT(21,25)\|COMMERCIAL ENTERPRISE(17,1)\|GIBBSITE(15,2)\|BINDER(14,3)\|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)\|NEODYMIUM(12,11)\|BRUKER PROPRIETARY GEO CALIBRATION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|LANTHANUM(11,9)\|SAMARIUM(11,8)\|SCANDIUM(11,8)\|YTTERBIUM(11,8)\|GADOLINIUM(11,7)\|PRASEODYMIUM(11,6)\|BERYLLIUM(11,2)\|GERMANIUM(11,2)\|RUBIDIUM(11,2)\|ZIRCONIUM(11,2)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|DRAWDOWN CALCULATION(10,4)\|VROCK MONTE CARLO SIMULATION(10,1)\|AVERAGE PARTICLE SIZE(9,4)\|ERW(9,4)\|BLAST FURNACE SLAG(9,2)\|CASO(9,2)\|CESIUM(9,2)\|CHROMIUM(9,2)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|RIGOROUS QUANTIFICATION(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|BIOLOGICAL DERIVED COMPONENT(9,1)\|PELLETIZED MINERAL AMENDMENT(9,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|GYPSUM(8,3)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|NONLIMITING CANDIDATE(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|STERILIZED SOIL BEAKER(8,1)\|TRANSITION METAL(7,5)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|COMPUTING VROCK(7,2)\|DISSOLUTION KINETICS(7,2)\|PHOSPHATE FERTILIZER(7,2)\|PULVERIZED SILICATE(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|CARBON FLUX(6,3)\|CHARGE IMBALANCE(6,2)\|INORGANIC ADDITIVE(6,2)\|MG PPM DETECTION(6,2)\|NEUTRAL GROUND(6,2)\|ROCK PARTICLE(6,2)\|VROCK DOT PRODUCT(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|AGGREGATED PELLET(6,1)\|AGLIME SUBSTITUTE(6,1)\|AGRICULTURAL SOILS(6,1)\|AGRONOMIC PERFORMANCE EXPECTATION(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|BIOFILM MEDIATING(6,1)\|CO2 REAGENT AVAILABILITY(6,1)\|CO2 UPTAKE(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|DDIC DTA ESTIMATE(6,1)\|FORSTERITE METRIC TON(6,1)\|FORSTERITE TENDENCY(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INFERRED ION FLUX(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|INTENSE SCRUTINY(6,1)\|MARKETING COLLATERAL(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|NONPROFIT ORGANIZATION(6,1)\|OCEAN ACIDIFICATION(6,1)\|PELLET AGGLOMERATION(6,1)\|PHOSPHORUS ECOSYSTEM LOSS(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|PREAPPLICATION SOIL(6,1)\|PROTONATED MICROBE(6,1)\|PULVERIZED LIMESTONE(6,1)\|PULVERIZED MG2SIO(6,1)\|RENOWNED CHEMIST(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|REWET BIOMASS(6,1)\|RIGOROUS COMPLIANCE(6,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)\|SOIL CULTIVATED ZONE(6,1)\|SOIL GEOCHEMISTRY(6,1)\|SOIL HYDROLOGY(6,1)\|NACL SOLUTION(5,4)\|PROMETHIUM(5,4)\|PULVERIZATION(5,4)\|TRIPLICATE(5,4)\|CENTRIFUGE CELL(5,3)\|BICARBONATE HCO3(5,2)\|AEROSOL SIZED PARTICLE(5,1)\|AGGREGATING GROUND MINERAL(5,1)\|ANALYTICAL LABORATORY(5,1)\|ANCIENT ROCK FORMATION(5,1)\|ANION CONSERVATION(5,1)\|CATEGORY REGULATION(5,1)\|CATION CONSERVATION(5,1)\|CLAUSE XII(5,1)\|DIFFERENCE VROCK VECTOR(5,1)\|DIFFERENCE VSOIL VECTOR(5,1)\|DISSOLVE ALGINATE(5,1)\|DISSOLVED ALGINATE POWDER(5,1)\|DOWNSTREAM ECOSYSTEM(5,1)\|DOWNSTREAM WATERWAY(5,1)\|DTA DH INVERSE(5,1)\|DUST PREVALENCE(5,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)\|FUNGAL ADJUVANT(5,1)\|GROUND MINERAL AGGREGATION(5,1)\|KEY INSIGHT(5,1)\|MICROBIAL CATION EXCHANGER(5,1)\|MINERAL ADJUVANT(5,1)\|MINERAL TON HECTARE(5,1)\|NUTRIENT AVAILABILITY(5,1)\|PELLET DISSOLUTION(5,1)\|PHOSPHATE ZINC PRECIPITATE(5,1)\|PROGRESS FRACTIONATION(5,1)\|QUASI GOVERNMENTAL REGULATOR(5,1)\|RESERVOIR GEOLOGY(5,1)\|SOIL STERILIZATION(5,1)\|SPECIALIZED TOOL(5,1)\|STEAM STERILIZATION(5,1)\|TECHNO ECONOMIC MODELING(5,1)\|ULTIMATE PRICE(5,1)\|UREY REACTION BASIC PREMISE(5,1)\|VERIFICATION VERSION(5,1)\|VERIFIED ENHANCED ROCK(5,1)\|VOLUNTARY MARKET(5,1)\|RARE EARTH ELEMENT(4,18)\|AQUEOUS CO2(4,2)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DISSOLUTION ENHANCING(4,1)\|DIVALENT MG(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|H2CO SUM(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|LB BROTH(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|REACTION THERMODYNAMICS(4,1)\|SECURITIZED CARBON REMOVAL(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|UNSEALING SAMPLE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|XRF ANALYSIS(4,1)\|BAG(3,2)\|CO2 REMOVAL(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|GROWING PLANT(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|SOIL SAMPLE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|CO2 MOLECULAR MASS(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|\|(US20230273174)\|MINERAL AMENDMENT(100,22)\|VERIFICATION(100,18)\|REMOVING CARBON(100,13)\|ENHANCED ROCK(100,8)\|SILICATE MINERAL AGGLOMERATION(66,2)\|COMMINUTED SILICATE MINERAL(57,3)\|ENHANCED ROCK WEATHERING(46,2)\|INTERESTED PARTY(45,1)\|FUNDAMENTAL ISSUE(37,1)\|MINERAL TRANSFORMATION(31,2)\|SAMPLING COLUMN(27,1)\|CARBON MEASUREMENT OBJECTIVE(25,1)\|LANDOWNER(23,1)\|SLOW RELEASE ACIDIFIER(22,3)\|IMMOBILE TRACE ELEMENT(21,25)\|COMMERCIAL ENTERPRISE(17,1)\|GIBBSITE(15,2)\|BINDER(14,3)\|NEODYMIUM(12,11)\|BRUKER PROPRIETARY GEO CALIBRATION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|LANTHANUM(11,9)\|SAMARIUM(11,8)\|SCANDIUM(11,8)\|YTTERBIUM(11,8)\|GADOLINIUM(11,7)\|PRASEODYMIUM(11,6)\|BERYLLIUM(11,2)\|GERMANIUM(11,2)\|RUBIDIUM(11,2)\|ZIRCONIUM(11,2)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|DRAWDOWN CALCULATION(10,4)\|VROCK MONTE CARLO SIMULATION(10,1)\|AVERAGE PARTICLE SIZE(9,4)\|ERW(9,4)\|BLAST FURNACE SLAG(9,2)\|CASO(9,2)\|CESIUM(9,2)\|CHROMIUM(9,2)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|RIGOROUS QUANTIFICATION(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|BIOLOGICAL DERIVED COMPONENT(9,1)\|DIVERSE DECARBONIZATION STRATEGY(9,1)\|PELLETIZED MINERAL AMENDMENT(9,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|GYPSUM(8,3)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|NONLIMITING CANDIDATE(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|STERILIZED SOIL BEAKER(8,1)\|TRANSITION METAL(7,5)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|COMPUTING VROCK(7,2)\|DISSOLUTION KINETICS(7,2)\|PHOSPHATE FERTILIZER(7,2)\|PULVERIZED SILICATE(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|CARBON FLUX(6,3)\|CHARGE IMBALANCE(6,2)\|INORGANIC ADDITIVE(6,2)\|MG PPM DETECTION(6,2)\|NEUTRAL GROUND(6,2)\|ROCK PARTICLE(6,2)\|VROCK DOT PRODUCT(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|AGGREGATED PELLET(6,1)\|AGLIME SUBSTITUTE(6,1)\|AGRICULTURAL SOILS(6,1)\|AGRONOMIC PERFORMANCE EXPECTATION(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|BIOFILM MEDIATING(6,1)\|CO2 REAGENT AVAILABILITY(6,1)\|CO2 UPTAKE(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|DDIC DTA ESTIMATE(6,1)\|FORSTERITE METRIC TON(6,1)\|FORSTERITE TENDENCY(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INFERRED ION FLUX(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|INTENSE SCRUTINY(6,1)\|MARKETING COLLATERAL(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|NONPROFIT ORGANIZATION(6,1)\|OCEAN ACIDIFICATION(6,1)\|PELLET AGGLOMERATION(6,1)\|PHOSPHORUS ECOSYSTEM LOSS(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|PREAPPLICATION SOIL(6,1)\|PROTONATED MICROBE(6,1)\|PULVERIZED LIMESTONE(6,1)\|PULVERIZED MG2SIO(6,1)\|RENOWNED CHEMIST(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|REWET BIOMASS(6,1)\|RIGOROUS COMPLIANCE(6,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(6,1)\|SOIL CULTIVATED ZONE(6,1)\|SOIL GEOCHEMISTRY(6,1)\|SOIL HYDROLOGY(6,1)\|NACL SOLUTION(5,4)\|PROMETHIUM(5,4)\|PULVERIZATION(5,4)\|TRIPLICATE(5,4)\|CENTRIFUGE CELL(5,3)\|BICARBONATE HCO3(5,2)\|GROWING PLANT(5,2)\|AEROSOL SIZED PARTICLE(5,1)\|AGGREGATING GROUND MINERAL(5,1)\|ANALYTICAL LABORATORY(5,1)\|ANCIENT ROCK FORMATION(5,1)\|ANION CONSERVATION(5,1)\|CATEGORY REGULATION(5,1)\|CATION CONSERVATION(5,1)\|CLAUSE XII(5,1)\|DIFFERENCE VROCK VECTOR(5,1)\|DIFFERENCE VSOIL VECTOR(5,1)\|DISSOLVE ALGINATE(5,1)\|DISSOLVED ALGINATE POWDER(5,1)\|DOWNSTREAM ECOSYSTEM(5,1)\|DOWNSTREAM WATERWAY(5,1)\|DTA DH INVERSE(5,1)\|DUST PREVALENCE(5,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(5,1)\|FUNGAL ADJUVANT(5,1)\|GROUND MINERAL AGGREGATION(5,1)\|KEY INSIGHT(5,1)\|MICROBIAL CATION EXCHANGER(5,1)\|MINERAL ADJUVANT(5,1)\|NUTRIENT AVAILABILITY(5,1)\|PELLET DISSOLUTION(5,1)\|PHOSPHATE ZINC PRECIPITATE(5,1)\|PROGRESS FRACTIONATION(5,1)\|QUASI GOVERNMENTAL REGULATOR(5,1)\|RESERVOIR GEOLOGY(5,1)\|SOIL STERILIZATION(5,1)\|SPECIALIZED TOOL(5,1)\|STEAM STERILIZATION(5,1)\|TECHNO ECONOMIC MODELING(5,1)\|ULTIMATE PRICE(5,1)\|VERIFICATION VERSION(5,1)\|VERIFIED ENHANCED ROCK(5,1)\|VOLUNTARY MARKET(5,1)\|RARE EARTH ELEMENT(4,18)\|AQUEOUS CO2(4,2)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DISSOLUTION ENHANCING(4,1)\|DIVALENT MG(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|H2CO SUM(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|LB BROTH(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|REACTION THERMODYNAMICS(4,1)\|SECURITIZED CARBON REMOVAL(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|UNSEALING SAMPLE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|XRF ANALYSIS(4,1)\|BAG(3,2)\|CO2 REMOVAL(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|SOIL SAMPLE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|CO2 MOLECULAR MASS(2,1)\|COMPACT MASS(2,1)\|\|(US11644454)\|MINERAL AMENDMENT(100,20)\|VERIFICATION(100,18)\|REMOVING CARBON(100,12)\|ENHANCED ROCK(100,8)\|ENHANCED ROCK WEATHERING(100,3)\|INTERESTED PARTY(42,1)\|FUNDAMENTAL ISSUE(35,1)\|IMMOBILE TRACE ELEMENT(33,30)\|SAMPLING COLUMN(26,1)\|CARBON MEASUREMENT OBJECTIVE(24,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(22,1)\|LANDOWNER(22,1)\|SOIL SAMPLE(21,10)\|DIVALENT CATION MEASUREMENT(20,2)\|COMMERCIAL ENTERPRISE(16,1)\|MINERAL AMENDMENT ADDITION(12,1)\|VANADIUM(12,1)\|NEODYMIUM(11,11)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|PRASEODYMIUM(11,6)\|BRUKER PROPRIETARY GEO CALIBRATION(11,1)\|LANTHANUM(10,9)\|SAMARIUM(10,8)\|SCANDIUM(10,8)\|YTTERBIUM(10,8)\|GADOLINIUM(10,7)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|BERYLLIUM(10,2)\|GERMANIUM(10,2)\|RUBIDIUM(10,2)\|ZIRCONIUM(10,2)\|DRAWDOWN CALCULATION(9,4)\|ERW(9,4)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(9,2)\|TANTALUM(9,2)\|VROCK MONTE CARLO SIMULATION(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE METAL(8,4)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|CESIUM(8,2)\|CHROMIUM(8,2)\|NONLIMITING CANDIDATE(8,2)\|RIGOROUS QUANTIFICATION(8,2)\|DELIVER PROSPECTIVE REWARD(8,1)\|DIVERSE DECARBONIZATION STRATEGY(8,1)\|PELLETIZED MINERAL AMENDMENT(8,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(8,1)\|STERILIZED SOIL BEAKER(8,1)\|ETHYLENEDIAMINETETRAACETIC ACID(7,4)\|PPB DETECTION(7,4)\|INSTRUMENTAL ERROR(7,3)\|PHOSPHATE FERTILIZER(7,2)\|ALKALIZER KINETICS(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|TRANSITION METAL(6,5)\|CARBON FLUX(6,3)\|APPLIED DIVALENT CATION(6,2)\|COMPUTING VROCK(6,2)\|DISSOLUTION KINETICS(6,2)\|PULVERIZED SILICATE(6,2)\|ROCK PARTICLE(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|CO2 REAGENT AVAILABILITY(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|FORSTERITE METRIC TON(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|PELLET AGGLOMERATION(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|CENTRIFUGE CELL(5,3)\|BICARBONATE HCO3(5,2)\|CHARGE IMBALANCE(5,2)\|GROWING PLANT(5,2)\|INORGANIC ADDITIVE(5,2)\|MG PPM DETECTION(5,2)\|NEUTRAL GROUND(5,2)\|VROCK DOT PRODUCT(5,2)\|AGGREGATED PELLET(5,1)\|AGLIME SUBSTITUTE(5,1)\|AGRICULTURAL SOILS(5,1)\|AGRONOMIC PERFORMANCE EXPECTATION(5,1)\|BIOFILM MEDIATING(5,1)\|CO2 UPTAKE(5,1)\|DDIC DTA ESTIMATE(5,1)\|FORSTERITE TENDENCY(5,1)\|INFERRED ION FLUX(5,1)\|INTENSE SCRUTINY(5,1)\|MARKETING COLLATERAL(5,1)\|NONPROFIT ORGANIZATION(5,1)\|OCEAN ACIDIFICATION(5,1)\|PHOSPHORUS ECOSYSTEM LOSS(5,1)\|PREAPPLICATION SOIL(5,1)\|PROTONATED MICROBE(5,1)\|PULVERIZED LIMESTONE(5,1)\|PULVERIZED MG2SIO(5,1)\|RENOWNED CHEMIST(5,1)\|REWET BIOMASS(5,1)\|RIGOROUS COMPLIANCE(5,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(5,1)\|SOIL CULTIVATED ZONE(5,1)\|SOIL GEOCHEMISTRY(5,1)\|SOIL HYDROLOGY(5,1)\|X RAY FLUORESCENCE SPECTROSCOPY(5,1)\|RARE EARTH ELEMENT(4,18)\|NACL SOLUTION(4,4)\|PROMETHIUM(4,4)\|PULVERIZATION(4,4)\|TRIPLICATE(4,4)\|AQUEOUS CO2(4,2)\|AVOIDED EMISSION(4,2)\|CARBONATE SPECIES(4,2)\|DISSOLVED CARBONATE(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SOIL ENVIRONMENT(4,2)\|ABUNDANT CO2(4,1)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AEROSOL SIZED PARTICLE(4,1)\|AGGREGATING GROUND MINERAL(4,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(4,1)\|ANALYTICAL LABORATORY(4,1)\|ANCIENT ROCK FORMATION(4,1)\|ANION CONSERVATION(4,1)\|AQUEOUS BICARBONATE MEASUREMENT(4,1)\|AQUEOUS COMPLEXATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|CATEGORY REGULATION(4,1)\|CATION CONSERVATION(4,1)\|CLAUSE XII(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|DIFFERENCE VROCK VECTOR(4,1)\|DIFFERENCE VSOIL VECTOR(4,1)\|DISSOLUTION ENHANCING(4,1)\|DISSOLVE ALGINATE(4,1)\|DISSOLVED ALGINATE POWDER(4,1)\|DIVALENT MG(4,1)\|DOWNSTREAM ECOSYSTEM(4,1)\|DOWNSTREAM WATERWAY(4,1)\|DTA DH INVERSE(4,1)\|DUST PREVALENCE(4,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|FUNGAL ADJUVANT(4,1)\|GROUND MINERAL AGGREGATION(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|H2CO SUM(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|KEY INSIGHT(4,1)\|LB BROTH(4,1)\|MICROBIAL CATION EXCHANGER(4,1)\|MINERAL ADJUVANT(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|NUTRIENT AVAILABILITY(4,1)\|PELLET DISSOLUTION(4,1)\|PHOSPHATE LEACHING(4,1)\|PHOSPHATE MOBILITY(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|PROGRESS FRACTIONATION(4,1)\|QUASI GOVERNMENTAL REGULATOR(4,1)\|REACTION THERMODYNAMICS(4,1)\|RESERVOIR GEOLOGY(4,1)\|SECURITIZED CARBON REMOVAL(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|SOIL STERILIZATION(4,1)\|SPECIALIZED TOOL(4,1)\|STEAM STERILIZATION(4,1)\|TECHNO ECONOMIC MODELING(4,1)\|ULTIMATE PRICE(4,1)\|UNSEALING SAMPLE(4,1)\|UREY REACTION BASIC PREMISE(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|VERIFICATION VERSION(4,1)\|VERIFIED ENHANCED ROCK(4,1)\|VOLUNTARY MARKET(4,1)\|XRF ANALYSIS(4,1)\|CARBON DIOXIDE REMOVAL(3,10)\|BAG(3,2)\|BINDER(3,2)\|CO2 REMOVAL(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|HEAVY PHOSPHATE(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PHOSPHATE ZINC PRECIPITATE(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SLOW RELEASE ACIDIFIER(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|4H4SIO(2,1)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|CO2 MOLECULAR MASS(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|\|(US20220404329)\|MINERAL AMENDMENT(100,30)\|VERIFICATION(100,17)\|REMOVING CARBON(100,13)\|ENHANCED ROCK(100,8)\|ENHANCED ROCK WEATHERING(100,3)\|SILICATE MINERAL AGGLOMERATION(46,2)\|COMMINUTED SILICATE MINERAL(39,3)\|IMMOBILE TRACE ELEMENT(32,34)\|INTERESTED PARTY(31,1)\|FUNDAMENTAL ISSUE(25,1)\|MINERAL TRANSFORMATION(21,2)\|ETHYLENE DIAMINE TETRAACETIC ACID(20,1)\|SAMPLING COLUMN(19,1)\|CARBON MEASUREMENT OBJECTIVE(18,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(16,1)\|LANDOWNER(16,1)\|SOIL SAMPLE(15,10)\|SLOW RELEASE ACIDIFIER(15,3)\|DIVALENT CATION MEASUREMENT(15,2)\|BERYLLIUM(12,3)\|VANADIUM(12,2)\|COMMERCIAL ENTERPRISE(12,1)\|DYSPROSIUM(11,10)\|GADOLINIUM(11,8)\|PRASEODYMIUM(11,7)\|GERMANIUM(11,3)\|RUBIDIUM(11,3)\|ZIRCONIUM(11,3)\|NEODYMIUM(10,12)\|EUROPIUM(10,11)\|LANTHANUM(10,10)\|SAMARIUM(10,9)\|SCANDIUM(10,9)\|YTTERBIUM(10,9)\|HOLMIUM(10,7)\|LUTETIUM(10,7)\|THULIUM(10,7)\|BINDER(10,3)\|GALLIUM(10,3)\|HAFNIUM(10,3)\|NIOBIUM(10,3)\|TANTALUM(10,3)\|GIBBSITE(10,2)\|RARE METAL(9,6)\|CESIUM(9,3)\|CHROMIUM(9,3)\|MINERAL AMENDMENT ADDITION(9,1)\|CERIUM(8,10)\|YTTRIUM(8,9)\|BRUKER PROPRIETARY GEO CALIBRATION(8,1)\|TRANSITION METAL(7,7)\|DRAWDOWN CALCULATION(7,4)\|VROCK MONTE CARLO SIMULATION(7,1)\|AVERAGE PARTICLE SIZE(6,4)\|ERW(6,4)\|GYPSUM(6,3)\|BLAST FURNACE SLAG(6,2)\|CASO(6,2)\|RIGOROUS QUANTIFICATION(6,2)\|SIO2 PERCENT MINERALOGICAL FRACTION(6,2)\|BIOLOGICAL DERIVED COMPONENT(6,1)\|DELIVER PROSPECTIVE REWARD(6,1)\|DIVERSE DECARBONIZATION STRATEGY(6,1)\|PELLETIZED MINERAL AMENDMENT(6,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(6,1)\|STERILIZED SOIL BEAKER(6,1)\|RARE EARTH ELEMENT(5,20)\|PPB DETECTION(5,4)\|INSTRUMENTAL ERROR(5,3)\|MINERAL SOIL AMENDMENT(5,3)\|AIRTIGHT CONTAINMENT(5,2)\|APPLIED DIVALENT CATION(5,2)\|COMPUTING VROCK(5,2)\|DISSOLUTION KINETICS(5,2)\|NONLIMITING CANDIDATE(5,2)\|PHOSPHATE FERTILIZER(5,2)\|PULVERIZED SILICATE(5,2)\|ALKALIZER KINETICS(5,1)\|MINERAL ADDITIVE PROVEN IDENTITY(5,1)\|SOIL ORGANIC CARBON(5,1)\|TAXONOMY DISTINGUISHE(5,1)\|UNINHABITABLE WATERWAY(5,1)\|WET BIOMASS WET ALIQUOT(5,1)\|CARBON FLUX(4,3)\|CENTRIFUGE CELL(4,3)\|CHARGE IMBALANCE(4,2)\|INORGANIC ADDITIVE(4,2)\|MG PPM DETECTION(4,2)\|NEUTRAL GROUND(4,2)\|ROCK PARTICLE(4,2)\|VROCK DOT PRODUCT(4,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(4,1)\|AGGREGATED PELLET(4,1)\|AGLIME SUBSTITUTE(4,1)\|AGRICULTURAL SOILS(4,1)\|AGRONOMIC PERFORMANCE EXPECTATION(4,1)\|ALKALINITY EXPORT(4,1)\|BIODEGRADABLE TRANSPORTER(4,1)\|BIOFILM MEDIATING(4,1)\|CO2 REAGENT AVAILABILITY(4,1)\|CO2 UPTAKE(4,1)\|CUMULATIVE CATION FLUX MEASURE(4,1)\|DDIC DTA ESTIMATE(4,1)\|FORSTERITE METRIC TON(4,1)\|FORSTERITE TENDENCY(4,1)\|HENRY LAW COEFFICIENT(4,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(4,1)\|INFERRED ION FLUX(4,1)\|INSTRUMENTAL UNCERTAINTY(4,1)\|INTENSE SCRUTINY(4,1)\|MARKETING COLLATERAL(4,1)\|MICRONUTRIENT INCORPORATION(4,1)\|MYCORRHIZAL INOCULUM(4,1)\|NONPROFIT ORGANIZATION(4,1)\|OCEAN ACIDIFICATION(4,1)\|PELLET AGGLOMERATION(4,1)\|PHOSPHORUS ECOSYSTEM LOSS(4,1)\|PORTABLE XRF INSTRUMENT(4,1)\|PREAPPLICATION SOIL(4,1)\|PROTONATED MICROBE(4,1)\|PULVERIZED LIMESTONE(4,1)\|PULVERIZED MG2SIO(4,1)\|RENOWNED CHEMIST(4,1)\|RESPIRATORY HEALTH IMPACT(4,1)\|REWET BIOMASS(4,1)\|RIGOROUS COMPLIANCE(4,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(4,1)\|SOIL CULTIVATED ZONE(4,1)\|SOIL GEOCHEMISTRY(4,1)\|SOIL HYDROLOGY(4,1)\|X RAY FLUORESCENCE SPECTROSCOPY(4,1)\|CARBON DIOXIDE REMOVAL(3,9)\|NACL SOLUTION(3,4)\|PROMETHIUM(3,4)\|PULVERIZATION(3,4)\|TRIPLICATE(3,4)\|AQUEOUS CO2(3,2)\|AVOIDED EMISSION(3,2)\|BICARBONATE HCO3(3,2)\|CARBONATE SPECIES(3,2)\|DISSOLVED CARBONATE(3,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(3,2)\|GROWING PLANT(3,2)\|MINERAL POTENTIAL(3,2)\|SECURE VESSEL(3,2)\|SOIL ENVIRONMENT(3,2)\|ABUNDANT CO2(3,1)\|ACCELERATE TIMING(3,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(3,1)\|AEROSOL SIZED PARTICLE(3,1)\|AGGREGATING GROUND MINERAL(3,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(3,1)\|ANALYTICAL LABORATORY(3,1)\|ANCIENT ROCK FORMATION(3,1)\|ANION CONSERVATION(3,1)\|AQUEOUS BICARBONATE MEASUREMENT(3,1)\|AQUEOUS COMPLEXATION(3,1)\|ASBESTOS EXPOSURE(3,1)\|ASSEMBLING MP(3,1)\|ATTENDANT DEMAND(3,1)\|AUXILIARY GEOCHEMICAL DATA(3,1)\|BICARBONATE MOLE(3,1)\|BROAD FRAMEWORK(3,1)\|CARBON EXCHANGE TRANSACTION(3,1)\|CARBON VERIFICATION BENEFIT(3,1)\|CATEGORY REGULATION(3,1)\|CATION CONSERVATION(3,1)\|CLAUSE XII(3,1)\|COARSE PARTICLE(3,1)\|COLLECT CELL PELLET(3,1)\|CONTINENTAL COLLISION RELEASE(3,1)\|CROP HEALTH(3,1)\|DIFFERENCE VROCK VECTOR(3,1)\|DIFFERENCE VSOIL VECTOR(3,1)\|DISSOLUTION ENHANCING(3,1)\|DISSOLVE ALGINATE(3,1)\|DISSOLVED ALGINATE POWDER(3,1)\|DIVALENT MG(3,1)\|DOWNSTREAM ECOSYSTEM(3,1)\|DOWNSTREAM WATERWAY(3,1)\|DTA DH INVERSE(3,1)\|DUST PREVALENCE(3,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(3,1)\|EQUILIBRIUM EQUATION(3,1)\|FERTILIZATION FREQUENCY(3,1)\|FRAUDULENT SAMPLE(3,1)\|FUNGAL ADJUVANT(3,1)\|GROUND MINERAL AGGREGATION(3,1)\|GROUND NATURAL ENVIRONMENT(3,1)\|H2CO SUM(3,1)\|INCREASE ECOSYSTEM COBENEFIT(3,1)\|KEY INSIGHT(3,1)\|LB BROTH(3,1)\|MICROBIAL CATION EXCHANGER(3,1)\|MINERAL ADJUVANT(3,1)\|MINERAL TRANSFORMATION EXTENT(3,1)\|MINUS PROTON DONOR(3,1)\|NUTRIENT AVAILABILITY(3,1)\|PELLET DISSOLUTION(3,1)\|PHOSPHATE LEACHING(3,1)\|PHOSPHATE MOBILITY(3,1)\|PRECISE ANSWER(3,1)\|PREEQUILIBRATED TUBE(3,1)\|PROGRESS FRACTIONATION(3,1)\|QUASI GOVERNMENTAL REGULATOR(3,1)\|REACTION THERMODYNAMICS(3,1)\|RESERVOIR GEOLOGY(3,1)\|SECURITIZED CARBON REMOVAL(3,1)\|SILICATE MINERAL SHELL(3,1)\|SILICATE ROLE(3,1)\|SOIL STERILIZATION(3,1)\|SPECIALIZED TOOL(3,1)\|STEAM STERILIZATION(3,1)\|TECHNO ECONOMIC MODELING(3,1)\|ULTIMATE PRICE(3,1)\|UNSEALING SAMPLE(3,1)\|UREY REACTION BASIC PREMISE(3,1)\|VERIFIABLE CARBON REMOVAL(3,1)\|VERIFICATION VERSION(3,1)\|VERIFIED ENHANCED ROCK(3,1)\|VOLUNTARY MARKET(3,1)\|XRF ANALYSIS(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|BAG(2,2)\|CO2 REMOVAL(2,2)\|COMMINUTION(2,2)\|FARMER(2,2)\|MARKET ABILITY(2,2)\|PELLETIZING(2,2)\|PRODUCT FORMULATION(2,2)\|STAKEHOLDER(2,2)\|TOTAL FORMULATION(2,2)\|ACIDIC ENVIRONMENT(2,1)\|ANALYTICAL PERFORMANCE(2,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(2,1)\|CARBON MARKET MATURATION(2,1)\|CARBON REMOVAL VERIFICATION(2,1)\|CARBON TRANSACTION(2,1)\|COMPUTING INDEX(2,1)\|CORTEVA CARBON(2,1)\|DRIED PELLET(2,1)\|EMPLACEMENT LOCATION(2,1)\|ENTIRE US ECONOMY(2,1)\|EXCHANGE COEFFICIENT(2,1)\|EXCHANGING RESIN(2,1)\|EXPERIMENTAL WORK(2,1)\|EXTANT FARM EQUIPMENT(2,1)\|FILTRATE ANALYSIS(2,1)\|FULL SUMMATION(2,1)\|GRIND CELL(2,1)\|HEAVY PHOSPHATE(2,1)\|ICP ANALYSIS(2,1)\|IMMOBILIZATION(2,1)\|INDIGO CARBON(2,1)\|LABORATORY SETTING(2,1)\|MARINE SETTING(2,1)\|MINERAL DELIVERY(2,1)\|MINERAL DISSOLUTION RATE(2,1)\|NATURAL ABUNDANCE CALCULATION(2,1)\|NATURAL SOILS(2,1)\|NEGATIVE EMISSION(2,1)\|PHOSPHATE ZINC PRECIPITATE(2,1)\|PLANT DEMAND(2,1)\|PROJECT EVALUATION CRITERIA(2,1)\|RELEVANT ION(2,1)\|ROCK ELEMENTAL ANALYSIS(2,1)\|ROCK MATERIAL ACCELERATED WEATHERING(2,1)\|SAMPLING DENSITY(2,1)\|SHARP THRESHOLD(2,1)\|SOIL ELEMENTAL ANALYSIS(2,1)\|SUBSURFACE SOIL PORE WATER(2,1)\|TECHNOLOGICAL SOLUTION(2,1)\|WET GRAM(2,1)\|ABILITY THRESHOLD(1,1)\|ACCEPTANCE(1,1)\|ACCOUNTING(1,1)\|ACID TREATED ARTHROBACTER(1,1)\|ACIDIC SOIL SOLUTION(1,1)\|ADDITIONALITY(1,1)\|ADMIXTURE(1,1)\|AERATION(1,1)\|AGLIME MESH SIZE OBSERVATION(1,1)\|AGRICULTURE(1,1)\|ALGAL BLOOM(1,1)\|ANALYTICAL SOLUTION(1,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(1,1)\|ATTRACTION(1,1)\|AUTOCLAVE(1,1)\|BACTERIA(1,1)\|BIOADSORBED METAL ACTIVE RELEASE(1,1)\|BIOFUEL(1,1)\|CA BEARING SILICATE(1,1)\|CA CONTENT(1,1)\|CALIBRATION STANDARD(1,1)\|CAPTURING CARBON(1,1)\|CATION EXCHANGE COLUMN(1,1)\|CHARGE BALANCE(1,1)\|CHELATOR(1,1)\|CHITOSAN(1,1)\|CLASSIFICATION(1,1)\|CLAWBACK(1,1)\|CLIMEWORK(1,1)\|\|(US20260016458)\|MINERAL AMENDMENT(100,20)\|VERIFICATION(100,17)\|REMOVING CARBON(100,12)\|ENHANCED ROCK(100,7)\|VERIFYING ENHANCED ROCK WEATHERING(70,1)\|IMMOBILE TRACE ELEMENT(55,11)\|ENHANCED ROCK WEATHERING(43,2)\|INTERESTED PARTY(42,1)\|RECOVERING SAMPLING COLUMN(36,1)\|FUNDAMENTAL ISSUE(35,1)\|CARBON MEASUREMENT OBJECTIVE(24,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(22,1)\|LANDOWNER(22,1)\|SOIL SAMPLE(21,10)\|DIVALENT CATION MEASUREMENT(20,2)\|COMMERCIAL ENTERPRISE(16,1)\|CATEGORIZING DIVERSE DECARBONIZATION STRATEGY(13,1)\|MINERAL AMENDMENT ADDITION(12,1)\|VANADIUM(12,1)\|EUROPIUM(11,10)\|DYSPROSIUM(11,9)\|PRASEODYMIUM(11,6)\|BRUKER PROPRIETARY GEO CALIBRATION(11,1)\|LANTHANUM(10,9)\|SAMARIUM(10,8)\|SCANDIUM(10,8)\|YTTERBIUM(10,8)\|GADOLINIUM(10,7)\|HOLMIUM(10,6)\|LUTETIUM(10,6)\|THULIUM(10,6)\|BERYLLIUM(10,2)\|GERMANIUM(10,2)\|RUBIDIUM(10,2)\|SIO PERCENT MINERALOGICAL FRACTION(10,2)\|ZIRCONIUM(10,2)\|DRAWDOWN CALCULATION(9,4)\|ERW(9,4)\|GALLIUM(9,2)\|HAFNIUM(9,2)\|NIOBIUM(9,2)\|REES PPB DETECTION(9,2)\|TANTALUM(9,2)\|ANDTHE TRANSITION METAL(9,1)\|DAC PROJECT RIGOROUS QUANTIFICATION(9,1)\|CERIUM(8,9)\|YTTRIUM(8,8)\|RARE EARTH ELEMENT(8,6)\|RARE METAL(8,4)\|MINERAL SOIL AMENDMENT(8,3)\|AIRTIGHT CONTAINMENT(8,2)\|CESIUM(8,2)\|CHROMIUM(8,2)\|ETHYLENEDIAMINETETRAACETIC ACID(8,2)\|NONLIMITING CANDIDATE(8,2)\|REE TRIPLICATE(8,2)\|CARBON DIOXIDE REMOVAL FRACTIONATION(8,1)\|DELIVER PROSPECTIVE REWARD(8,1)\|PELLETIZED MINERAL AMENDMENT(8,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(8,1)\|STERILIZED SOIL BEAKER(8,1)\|INSTRUMENTAL ERROR(7,3)\|PHOSPHATE FERTILIZER(7,2)\|ALKALIZER KINETICS(7,1)\|DAC ULTIMATE PRICE(7,1)\|MINERAL ADDITIVE PROVEN IDENTITY(7,1)\|PHOSPHATE LEACHING LIKELIHOOD(7,1)\|SOIL ORGANIC CARBON(7,1)\|TAXONOMY DISTINGUISHE(7,1)\|UNINHABITABLE WATERWAY(7,1)\|WET BIOMASS WET ALIQUOT(7,1)\|TRANSITION METAL(6,5)\|CARBON FLUX(6,3)\|APPLIED DIVALENT CATION(6,2)\|CDR CALCULATION(6,2)\|DISSOLUTION KINETICS(6,2)\|PULVERIZED SILICATE(6,2)\|ROCK PARTICLE(6,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(6,1)\|ALKALINITY EXPORT(6,1)\|BIODEGRADABLE TRANSPORTER(6,1)\|CUMULATIVE CATION FLUX MEASURE(6,1)\|FORSTERITE METRIC TON(6,1)\|HENRY LAW COEFFICIENT(6,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(6,1)\|INSTRUMENTAL UNCERTAINTY(6,1)\|ITE FINGERPRINT(6,1)\|ITES ABUNDANCE(6,1)\|MICRONUTRIENT INCORPORATION(6,1)\|MYCORRHIZAL INOCULUM(6,1)\|PELLET AGGLOMERATION(6,1)\|PORTABLE XRF INSTRUMENT(6,1)\|RESPIRATORY HEALTH IMPACT(6,1)\|CENTRIFUGE CELL(5,3)\|CHARGE IMBALANCE(5,2)\|GROWING PLANT(5,2)\|INORGANIC ADDITIVE(5,2)\|MG PPM DETECTION(5,2)\|NEUTRAL GROUND(5,2)\|AGGREGATED PELLET(5,1)\|AGLIME SUBSTITUTE(5,1)\|AGRICULTURAL SOILS(5,1)\|AGRONOMIC PERFORMANCE EXPECTATION(5,1)\|BIOFILM MEDIATING(5,1)\|DDIC DTA ESTIMATE(5,1)\|DRAWDOWN ESTIMATION(5,1)\|FORSTERITE TENDENCY(5,1)\|INFERRED ION FLUX(5,1)\|INTENSE SCRUTINY(5,1)\|ITES PROPORTION(5,1)\|MARKETING COLLATERAL(5,1)\|NEGATIVELY CHARGED BICARBONATE(5,1)\|NONPROFIT ORGANIZATION(5,1)\|OCEAN ACIDIFICATION(5,1)\|PHOSPHORUS ECOSYSTEM LOSS(5,1)\|PREAPPLICATION SOIL(5,1)\|PROTONATED MICROBE(5,1)\|PULVERIZED LIMESTONE(5,1)\|RENOWNED CHEMIST(5,1)\|REWET BIOMASS(5,1)\|RIGOROUS COMPLIANCE(5,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(5,1)\|SOIL CULTIVATED ZONE(5,1)\|SOIL GEOCHEMISTRY(5,1)\|SOIL HYDROLOGY(5,1)\|X RAY FLUORESCENCE SPECTROSCOPY(5,1)\|NACL SOLUTION(4,4)\|PROMETHIUM(4,4)\|PULVERIZATION(4,4)\|AVOIDED EMISSION(4,2)\|CARBONATE DISSOLUTION(4,2)\|CARBONATE SPECIES(4,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(4,2)\|MARKET ABILITY(4,2)\|MINERAL POTENTIAL(4,2)\|SECURE VESSEL(4,2)\|SOIL ENVIRONMENT(4,2)\|ACCELERATE TIMING(4,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(4,1)\|AEROSOL SIZED PARTICLE(4,1)\|AGGREGATING GROUND MINERAL(4,1)\|ANALYTICAL LABORATORY(4,1)\|ANCIENT ROCK FORMATION(4,1)\|ANION CONSERVATION(4,1)\|ASBESTOS EXPOSURE(4,1)\|ASSEMBLING MP(4,1)\|ATTENDANT DEMAND(4,1)\|AUXILIARY GEOCHEMICAL DATA(4,1)\|BICARBONATE MOLE(4,1)\|BROAD FRAMEWORK(4,1)\|CARBON EXCHANGE TRANSACTION(4,1)\|CARBON VERIFICATION BENEFIT(4,1)\|CATEGORY REGULATION(4,1)\|CATION CONSERVATION(4,1)\|CLAUSE XII(4,1)\|COARSE PARTICLE(4,1)\|COLLECT CELL PELLET(4,1)\|CONTINENTAL COLLISION RELEASE(4,1)\|CROP HEALTH(4,1)\|CUSTOM ITE STANDARD(4,1)\|DISSOLUTION ENHANCING(4,1)\|DISSOLVE ALGINATE(4,1)\|DISSOLVED ALGINATE(4,1)\|DIVALENT MG(4,1)\|DOWNSTREAM ECOSYSTEM(4,1)\|DOWNSTREAM WATERWAY(4,1)\|DTA DH INVERSE(4,1)\|DUST PREVALENCE(4,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(4,1)\|EQUILIBRIUM EQUATION(4,1)\|FERTILIZATION FREQUENCY(4,1)\|FRAUDULENT SAMPLE(4,1)\|FUNGAL ADJUVANT(4,1)\|GROUND MINERAL AGGREGATION(4,1)\|GROUND NATURAL ENVIRONMENT(4,1)\|HEAVY PHOSPHATE(4,1)\|HEAVY REES(4,1)\|INCREASE ECOSYSTEM COBENEFIT(4,1)\|KEY INSIGHT(4,1)\|LB BROTH(4,1)\|MICROBIAL CATION EXCHANGER(4,1)\|MINERAL ADJUVANT(4,1)\|MINERAL TON HECTARE(4,1)\|MINERAL TRANSFORMATION EXTENT(4,1)\|MINUS PROTON DONOR(4,1)\|NATIVE ITE(4,1)\|NUTRIENT AVAILABILITY(4,1)\|PELLET DISSOLUTION(4,1)\|PHOSPHATE MOBILITY(4,1)\|PPM NEODYMIUM(4,1)\|PRECISE ANSWER(4,1)\|PREEQUILIBRATED TUBE(4,1)\|PROGRESS FRACTIONATION(4,1)\|PULVERIZED MG(4,1)\|QUASI GOVERNMENTAL REGULATOR(4,1)\|REACTION THERMODYNAMICS(4,1)\|REE AQUEOUS COMPLEXATION(4,1)\|REES FULL RECOVERY(4,1)\|RESERVOIR GEOLOGY(4,1)\|SILICATE MINERAL SHELL(4,1)\|SILICATE ROLE(4,1)\|SOIL STERILIZATION(4,1)\|SPECIALIZED TOOL(4,1)\|STEAM STERILIZATION(4,1)\|TECHNICAL CDR(4,1)\|TECHNO ECONOMIC MODELING(4,1)\|UNSEALING SAMPLE(4,1)\|UREY REACTION BASIC PREMISE(4,1)\|V MONTE CARLO SIMULATION(4,1)\|VERIFIABLE CARBON REMOVAL(4,1)\|VERIFICATION VERSION(4,1)\|VERIFIED ENHANCED ROCK(4,1)\|VOLUNTARY MARKET(4,1)\|XRF ANALYSIS(4,1)\|HCO(3,4)\|K2H(3,4)\|BAG(3,2)\|BINDER(3,2)\|COMMINUTION(3,2)\|FARMER(3,2)\|PELLETIZING(3,2)\|PRODUCT FORMULATION(3,2)\|STAKEHOLDER(3,2)\|TOTAL FORMULATION(3,2)\|ACIDIC ENVIRONMENT(3,1)\|ANALYTICAL PERFORMANCE(3,1)\|AQUEOUS BICARBONATE(3,1)\|CARBON MARKET MATURATION(3,1)\|CARBON REMOVAL VERIFICATION(3,1)\|CARBON TRANSACTION(3,1)\|COMPUTING INDEX(3,1)\|CORTEVA CARBON(3,1)\|DRIED PELLET(3,1)\|EMPLACEMENT LOCATION(3,1)\|ENTIRE US ECONOMY(3,1)\|EXCHANGE COEFFICIENT(3,1)\|EXCHANGING RESIN(3,1)\|EXPERIMENTAL WORK(3,1)\|EXTANT FARM EQUIPMENT(3,1)\|FILTRATE ANALYSIS(3,1)\|FULL SUMMATION(3,1)\|GRIND CELL(3,1)\|ICP ANALYSIS(3,1)\|IMMOBILIZATION(3,1)\|INDIGO CARBON(3,1)\|ITES COST(3,1)\|LABORATORY SETTING(3,1)\|MARINE SETTING(3,1)\|MINERAL DELIVERY(3,1)\|MINERAL DISSOLUTION RATE(3,1)\|NATURAL ABUNDANCE CALCULATION(3,1)\|NATURAL SOILS(3,1)\|NEGATIVE EMISSION(3,1)\|PHOSPHATE ZINC PRECIPITATE(3,1)\|PLANT DEMAND(3,1)\|PROJECT EVALUATION CRITERIA(3,1)\|RELEVANT ION(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|ROCK MATERIAL ACCELERATED WEATHERING(3,1)\|SAMPLING DENSITY(3,1)\|SHARP THRESHOLD(3,1)\|SLOW RELEASE ACIDIFIER(3,1)\|SOIL ELEMENTAL ANALYSIS(3,1)\|SUBSURFACE SOIL PORE WATER(3,1)\|TECHNOLOGICAL SOLUTION(3,1)\|WET GRAM(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|K1H(2,3)\|LYSE(2,3)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|CLAWBACK(2,1)\|CLIMEWORK(2,1)\|COMPACT MASS(2,1)\|COMPREHENSIVE PROPOSAL NUMBER(2,1)\|\|(WO2022/271842)\|MINERAL AMENDMENT(100,30)\|VERIFICATION(100,19)\|REMOVING CARBON(100,14)\|ENHANCED ROCK(100,10)\|ENHANCED ROCK WEATHERING(100,3)\|SILICATE MINERAL AGGLOMERATION(46,2)\|COMMINUTED SILICATE MINERAL(39,3)\|IMMOBILE TRACE ELEMENT(32,34)\|INTERESTED PARTY(31,1)\|FUNDAMENTAL ISSUE(25,1)\|SAMPLING COLUMN(19,1)\|CARBON MEASUREMENT OBJECTIVE(18,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(16,1)\|LANDOWNER(16,1)\|SOIL SAMPLE(15,10)\|SLOW RELEASE ACIDIFIER(15,3)\|DIVALENT CATION MEASUREMENT(15,2)\|BERYLLIUM(12,3)\|VANADIUM(12,2)\|COMMERCIAL ENTERPRISE(12,1)\|DYSPROSIUM(11,10)\|GADOLINIUM(11,8)\|PRASEODYMIUM(11,7)\|GERMANIUM(11,3)\|RUBIDIUM(11,3)\|ZIRCONIUM(11,3)\|NEODYMIUM(10,12)\|EUROPIUM(10,11)\|LANTHANUM(10,10)\|SAMARIUM(10,9)\|SCANDIUM(10,9)\|YTTERBIUM(10,9)\|HOLMIUM(10,7)\|LUTETIUM(10,7)\|THULIUM(10,7)\|BINDER(10,3)\|GALLIUM(10,3)\|HAFNIUM(10,3)\|NIOBIUM(10,3)\|TANTALUM(10,3)\|GIBBSITE(10,2)\|RARE METAL(9,6)\|CESIUM(9,3)\|CHROMIUM(9,3)\|MINERAL AMENDMENT ADDITION(9,1)\|CERIUM(8,10)\|YTTRIUM(8,9)\|BRUKER PROPRIETARY GEO CALIBRATION(8,1)\|TRANSITION METAL(7,7)\|DRAWDOWN CALCULATION(7,4)\|ETHYLENEDIAMINETETRAACETIC ACID(7,1)\|VR0CK MONTE CARLO SIMULATION(7,1)\|AVERAGE PARTICLE SIZE(6,4)\|ERW(6,4)\|GYPSUM(6,3)\|MINERAL SOIL AMENDMENT(6,3)\|BLAST FURNACE SLAG(6,2)\|RIGOROUS QUANTIFICATION(6,2)\|BIOLOGICAL DERIVED COMPONENT(6,1)\|DDIC DH DTA(6,1)\|DELIVER PROSPECTIVE REWARD(6,1)\|DIVERSE DECARBONIZATION STRATEGY(6,1)\|PELLETIZED MINERAL AMENDMENT(6,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(6,1)\|STERILIZED SOIL BEAKER(6,1)\|RARE EARTH ELEMENT(5,20)\|PPB DETECTION(5,4)\|INSTRUMENTAL ERROR(5,3)\|AIRTIGHT CONTAINMENT(5,2)\|APPLIED DIVALENT CATION(5,2)\|COMPUTING VROCK(5,2)\|DISSOLUTION KINETICS(5,2)\|NONLIMITING CANDIDATE(5,2)\|PHOSPHATE FERTILIZER(5,2)\|PULVERIZED SILICATE(5,2)\|SI PERCENT MINERALOGICAL FRACTION(5,2)\|ALKALIZER KINETICS(5,1)\|MINERAL ADDITIVE PROVEN IDENTITY(5,1)\|SOIL ORGANIC CARBON(5,1)\|TAXONOMY DISTINGUISHE(5,1)\|UNINHABITABLE WATERWAY(5,1)\|WET BIOMASS WET ALIQUOT(5,1)\|CARBON FLUX(4,3)\|CENTRIFUGE CELL(4,3)\|CHARGE IMBALANCE(4,2)\|INORGANIC ADDITIVE(4,2)\|MG PPM DETECTION(4,2)\|NEUTRAL GROUND(4,2)\|ROCK PARTICLE(4,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(4,1)\|AGGREGATED PELLET(4,1)\|AGLIME SUBSTITUTE(4,1)\|AGRICULTURAL SOILS(4,1)\|AGRONOMIC PERFORMANCE EXPECTATION(4,1)\|ALKALINITY EXPORT(4,1)\|BIODEGRADABLE TRANSPORTER(4,1)\|BIOFILM MEDIATING(4,1)\|CO2 REAGENT AVAILABILITY(4,1)\|CO2 UPTAKE(4,1)\|CUMULATIVE CATION FLUX MEASURE(4,1)\|DDIC DTA ESTIMATE(4,1)\|DRAWDOWN ESTIMATION(4,1)\|FORSTERITE METRIC TON(4,1)\|FORSTERITE TENDENCY(4,1)\|HENRY LAW COEFFICIENT(4,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(4,1)\|INFERRED ION FLUX(4,1)\|INSTRUMENTAL UNCERTAINTY(4,1)\|INTENSE SCRUTINY(4,1)\|MARKETING COLLATERAL(4,1)\|MICRONUTRIENT INCORPORATION(4,1)\|MYCORRHIZAL INOCULUM(4,1)\|NEGATIVELY CHARGED BICARBONATE(4,1)\|NONPROFIT ORGANIZATION(4,1)\|OCEAN ACIDIFICATION(4,1)\|PELLET AGGLOMERATION(4,1)\|PHOSPHORUS ECOSYSTEM LOSS(4,1)\|PORTABLE XRF INSTRUMENT(4,1)\|PREAPPLICATION SOIL(4,1)\|PROTONATED MICROBE(4,1)\|PULVERIZED LIMESTONE(4,1)\|PULVERIZED MGISICE(4,1)\|RENOWNED CHEMIST(4,1)\|RESPIRATORY HEALTH IMPACT(4,1)\|REWET BIOMASS(4,1)\|RIGOROUS COMPLIANCE(4,1)\|RLE TRIPLICATE(4,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(4,1)\|SOIL CULTIVATED ZONE(4,1)\|SOIL GEOCHEMISTRY(4,1)\|SOIL HYDROLOGY(4,1)\|X RAY FLUORESCENCE SPECTROSCOPY(4,1)\|CARBON DIOXIDE REMOVAL(3,9)\|NACL SOLUTION(3,4)\|PROMETHIUM(3,4)\|PULVERIZATION(3,4)\|AQUEOUS CO2(3,2)\|AVOIDED EMISSION(3,2)\|CARBONATE SPECIES(3,2)\|DISSOLVED CARBONATE(3,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(3,2)\|GROWING PLANT(3,2)\|MINERAL POTENTIAL(3,2)\|SECURE VESSEL(3,2)\|SOIL ENVIRONMENT(3,2)\|ACCELERATE TIMING(3,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(3,1)\|AEROSOL SIZED PARTICLE(3,1)\|AGGREGATING GROUND MINERAL(3,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(3,1)\|ANALYTICAL LABORATORY(3,1)\|ANCIENT ROCK FORMATION(3,1)\|ANION CONSERVATION(3,1)\|AQUEOUS BICARBONATE MEASUREMENT(3,1)\|AQUEOUS COMPLEXATION(3,1)\|ASBESTOS EXPOSURE(3,1)\|ASSEMBLING MP(3,1)\|ATTENDANT DEMAND(3,1)\|AUXILIARY GEOCHEMICAL DATA(3,1)\|BICARBONATE MOLE(3,1)\|BROAD FRAMEWORK(3,1)\|CARBON EXCHANGE TRANSACTION(3,1)\|CARBON VERIFICATION BENEFIT(3,1)\|CATEGORY REGULATION(3,1)\|CATION CONSERVATION(3,1)\|CLAUSE XII(3,1)\|COARSE PARTICLE(3,1)\|CONTINENTAL COLLISION RELEASE(3,1)\|CROP HEALTH(3,1)\|DIFFERENCE VR0CK VECTOR(3,1)\|DIFFERENCE VSOU VECTOR(3,1)\|DISSOLUTION ENHANCING(3,1)\|DISSOLVE ALGINATE(3,1)\|DISSOLVED ALGINATE POWDER(3,1)\|DIVALENT MG(3,1)\|DOWNSTREAM ECOSYSTEM(3,1)\|DOWNSTREAM WATERWAY(3,1)\|DTA DH INVERSE(3,1)\|DUST PREVALENCE(3,1)\|ECOSYSTEM CO BENEFIT(3,1)\|EQUILIBRIUM EQUATION(3,1)\|FERTILIZATION FREQUENCY(3,1)\|FRAUDULENT SAMPLE(3,1)\|FUNGAL ADJUVANT(3,1)\|GROUND MINERAL AGGREGATION(3,1)\|GROUND NATURAL ENVIRONMENT(3,1)\|H2CO SUM(3,1)\|INCREASE ECOSYSTEM COBENEFIT(3,1)\|KEY INSIGHT(3,1)\|LB BROTH(3,1)\|MICROBIAL CATION EXCHANGER(3,1)\|MINERAL ADJUVANT(3,1)\|MINERAL TRANSFORMATION EXTENT(3,1)\|MINUS PROTON DONOR(3,1)\|NUTRIENT AVAILABILITY(3,1)\|PELLET DISSOLUTION(3,1)\|PHOSPHATE LEACHING(3,1)\|PHOSPHATE MOBILITY(3,1)\|PRECISE ANSWER(3,1)\|PREEQUILIBRATED TUBE(3,1)\|PROGRESS FRACTIONATION(3,1)\|QUASI GOVERNMENTAL REGULATOR(3,1)\|REACTION THERMODYNAMICS(3,1)\|RESERVOIR GEOLOGY(3,1)\|SECURITIZED CARBON REMOVAL(3,1)\|SILICATE MINERAL SHELL(3,1)\|SILICATE ROLE(3,1)\|SOIL STERILIZATION(3,1)\|SPECIALIZED TOOL(3,1)\|STEAM STERILIZATION(3,1)\|STYRENE DIVINYLBENZENE(3,1)\|TECHNO ECONOMIC MODELING(3,1)\|TREATMENT UNIFORMITY(3,1)\|ULTIMATE PRICE(3,1)\|UNSEALING SAMPLE(3,1)\|UREY REACTION BASIC PREMISE(3,1)\|VERIFIABLE CARBON REMOVAL(3,1)\|VERIFICATION VERSION(3,1)\|VERIFIED ENHANCED ROCK(3,1)\|VOLUNTARY MARKET(3,1)\|VROCK DOT PRODUCT(3,1)\|XRF ANALYSIS(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|BAG(2,2)\|CO2 REMOVAL(2,2)\|FARMER(2,2)\|MARKET ABILITY(2,2)\|PELLETIZING(2,2)\|PRODUCT FORMULATION(2,2)\|STAKEHOLDER(2,2)\|TOTAL FORMULATION(2,2)\|ACIDIC ENVIRONMENT(2,1)\|ANALYTICAL PERFORMANCE(2,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(2,1)\|CARBON MARKET MATURATION(2,1)\|CARBON REMOVAL VERIFICATION(2,1)\|CARBON TRANSACTION(2,1)\|CELL PELLET(2,1)\|COMPUTING INDEX(2,1)\|CORTEVA CARBON(2,1)\|DRIED PELLET(2,1)\|EMPLACEMENT LOCATION(2,1)\|ENHANCED ROCK VARIABLE PERFORMANCE(2,1)\|ENTIRE US ECONOMY(2,1)\|EXCHANGE COEFFICIENT(2,1)\|EXCHANGING RESIN(2,1)\|EXPERIMENTAL WORK(2,1)\|EXTANT FARM EQUIPMENT(2,1)\|FILTRATE ANALYSIS(2,1)\|FULL SUMMATION(2,1)\|GRIND CELL(2,1)\|HEAVY PHOSPHATE(2,1)\|ICP ANALYSIS(2,1)\|IMMOBILIZATION(2,1)\|INDIGO CARBON(2,1)\|LABORATORY SETTING(2,1)\|MARINE SETTING(2,1)\|MINERAL DELIVERY(2,1)\|MINERAL DISSOLUTION RATE(2,1)\|NATURAL ABUNDANCE CALCULATION(2,1)\|NATURAL SOILS(2,1)\|NEGATIVE EMISSION(2,1)\|PHOSPHATE ZINC PRECIPITATE(2,1)\|PLANT DEMAND(2,1)\|PROJECT EVALUATION CRITERIA(2,1)\|RELEVANT ION(2,1)\|ROCK ELEMENTAL ANALYSIS(2,1)\|ROCK MATERIAL ACCELERATED WEATHERING(2,1)\|SAMPLING DENSITY(2,1)\|SHARP THRESHOLD(2,1)\|SOIL ELEMENTAL ANALYSIS(2,1)\|SUBSURFACE SOIL PORE WATER(2,1)\|TECHNOLOGICAL SOLUTION(2,1)\|WET GRAM(2,1)\|ABILITY THRESHOLD(1,1)\|ACCEPTANCE(1,1)\|ACCOUNTING(1,1)\|ACID TREATED ARTHROBACTER(1,1)\|ACIDIC SOIL SOLUTION(1,1)\|ADDITIONALITY(1,1)\|ADMIXTURE(1,1)\|AERATION(1,1)\|AGLIME MESH SIZE OBSERVATION(1,1)\|AGRICULTURE(1,1)\|ALGAL BLOOM(1,1)\|ANALYTICAL SOLUTION(1,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(1,1)\|ARACTUAI(1,1)\|ATTRACTION(1,1)\|AUTOCLAVE(1,1)\|BACTERIA(1,1)\|BIOADSORBED METAL ACTIVE RELEASE(1,1)\|BIOFUEL(1,1)\|CA BEARING SILICATE(1,1)\|CA CONTENT(1,1)\|CALIBRATION STANDARD(1,1)\|CAPTURING CARBON(1,1)\|CATION EXCHANGE COLUMN(1,1)\|CHARGE BALANCE(1,1)\|CHELATOR(1,1)\|CHITOSAN(1,1)\|CLASSIFICATION(1,1)\|CLAWBACK(1,1)\|CLIMEWORK(1,1)\|CO2 MOLECULAR MASS(1,1)\|\|(CA3207124)\|MINERAL AMENDMENT(100,28)\|ENHANCED ROCK(100,8)\|ENHANCED ROCK WEATHERING(100,2)\|SILICATE MINERAL AGGLOMERATION(51,2)\|COMMINUTED SILICATE MINERAL(44,3)\|INTERESTED PARTY(34,1)\|IMMOBILE TRACE ELEMENT(33,33)\|FUNDAMENTAL ISSUE(28,1)\|MINERAL TRANSFORMATION(24,2)\|ETHYLENE DIAMINE TETRAACETIC ACID(22,1)\|SAMPLING COLUMN(21,1)\|CARBON MEASUREMENT OBJECTIVE(20,1)\|IMMOBILE TRACE ELEMENT ABUNDANCE(18,1)\|LANDOWNER(18,1)\|SOIL SAMPLE(17,10)\|SLOW RELEASE ACIDIFIER(17,3)\|DIVALENT CATION MEASUREMENT(17,2)\|VERIFICATION(14,18)\|VANADIUM(14,2)\|BERYLLIUM(13,3)\|COMMERCIAL ENTERPRISE(13,1)\|DYSPROSIUM(12,10)\|GADOLINIUM(12,8)\|PRASEODYMIUM(12,7)\|GERMANIUM(12,3)\|RUBIDIUM(12,3)\|ZIRCONIUM(12,3)\|NEODYMIUM(11,12)\|EUROPIUM(11,11)\|LANTHANUM(11,10)\|SAMARIUM(11,9)\|SCANDIUM(11,9)\|YTTERBIUM(11,9)\|HOLMIUM(11,7)\|LUTETIUM(11,7)\|THULIUM(11,7)\|BINDER(11,3)\|GALLIUM(11,3)\|HAFNIUM(11,3)\|NIOBIUM(11,3)\|TANTALUM(11,3)\|GIBBSITE(11,2)\|RARE METAL(10,6)\|CESIUM(10,3)\|CHROMIUM(10,3)\|MINERAL AMENDMENT ADDITION(10,1)\|CERIUM(9,10)\|YTTRIUM(9,9)\|BRUKER PROPRIETARY GEO CALIBRATION(9,1)\|REMOVING CARBON(8,13)\|TRANSITION METAL(8,7)\|DRAWDOWN CALCULATION(8,4)\|VROCK MONTE CARLO SIMULATION(8,1)\|AVERAGE PARTICLE SIZE(7,4)\|ERW(7,4)\|BLAST FURNACE SLAG(7,2)\|CASO(7,2)\|RIGOROUS QUANTIFICATION(7,2)\|BIOLOGICAL DERIVED COMPONENT(7,1)\|DIVERSE DECARBONIZATION STRATEGY(7,1)\|PELLETIZED MINERAL AMENDMENT(7,1)\|SCIENCE SUPPORTIVE ECOSYSTEM(7,1)\|RARE EARTH ELEMENT(6,20)\|PPB DETECTION(6,4)\|GYPSUM(6,3)\|MINERAL SOIL AMENDMENT(6,3)\|AIRTIGHT CONTAINMENT(6,2)\|NONLIMITING CANDIDATE(6,2)\|PHOSPHATE FERTILIZER(6,2)\|SI PERCENT MINERALOGICAL FRACTION(6,2)\|ALKALIZER KINETICS(6,1)\|DELIVER PROSPECTIVE REWARD(6,1)\|MINERAL ADDITIVE PROVEN IDENTITY(6,1)\|NEGATIVELY CHARGED BICARBONATE HCO(6,1)\|SOIL ORGANIC CARBON(6,1)\|STERILIZED SOIL BEAKER(6,1)\|TAXONOMY DISTINGUISHE(6,1)\|UNINHABITABLE WATERWAY(6,1)\|WET BIOMASS WET ALIQUOT(6,1)\|CARBON FLUX(5,3)\|INSTRUMENTAL ERROR(5,3)\|APPLIED DIVALENT CATION(5,2)\|COMPUTING VROCK(5,2)\|DISSOLUTION KINETICS(5,2)\|PULVERIZED SILICATE(5,2)\|ROCK PARTICLE(5,2)\|ACCELERATE ROCK CRYSTAL LATTICE BREAKDOWN(5,1)\|ALKALINITY EXPORT(5,1)\|BIODEGRADABLE TRANSPORTER(5,1)\|CO2 REAGENT AVAILABILITY(5,1)\|CUMULATIVE CATION FLUX MEASURE(5,1)\|HENRY LAW COEFFICIENT(5,1)\|INDUCTIVELY COUPLED PLASMA SPECTROSCOPY(5,1)\|INSTRUMENTAL UNCERTAINTY(5,1)\|MICRONUTRIENT INCORPORATION(5,1)\|MYCORRHIZAL INOCULUM(5,1)\|PELLET AGGLOMERATION(5,1)\|PORTABLE XRF INSTRUMENT(5,1)\|RESPIRATORY HEALTH IMPACT(5,1)\|NACL SOLUTION(4,4)\|PROMETHIUM(4,4)\|PULVERIZATION(4,4)\|TRIPLICATE(4,4)\|CENTRIFUGE CELL(4,3)\|CHARGE IMBALANCE(4,2)\|GROWING PLANT(4,2)\|INORGANIC ADDITIVE(4,2)\|MG PPM DETECTION(4,2)\|NEUTRAL GROUND(4,2)\|VROCK DOT PRODUCT(4,2)\|AEROSOL SIZED PARTICLE(4,1)\|AGGREGATED PELLET(4,1)\|AGGREGATING GROUND MINERAL(4,1)\|AGLIME SUBSTITUTE(4,1)\|AGRICULTURAL SOILS(4,1)\|AGRONOMIC PERFORMANCE EXPECTATION(4,1)\|ANALYTICAL LABORATORY(4,1)\|ANCIENT ROCK FORMATION(4,1)\|ANION CONSERVATION(4,1)\|BIOFILM MEDIATING(4,1)\|CATEGORY REGULATION(4,1)\|CATION CONSERVATION(4,1)\|CLAUSE XII(4,1)\|CO2 UPTAKE(4,1)\|DDIC DTA ESTIMATE(4,1)\|DIFFERENCE VROCK VECTOR(4,1)\|DISSOLVE ALGINATE(4,1)\|DISSOLVED ALGINATE POWDER(4,1)\|DOWNSTREAM ECOSYSTEM(4,1)\|DOWNSTREAM WATERWAY(4,1)\|DTA DH INVERSE(4,1)\|DUST PREVALENCE(4,1)\|ENHANCED ROCK FINANCIAL PERFORMANCE(4,1)\|FORSTERITE MOLE(4,1)\|FORSTERITE TENDENCY(4,1)\|FUNGAL ADJUVANT(4,1)\|GROUND MINERAL AGGREGATION(4,1)\|INFERRED ION FLUX(4,1)\|INTENSE SCRUTINY(4,1)\|KEY INSIGHT(4,1)\|MARKETING COLLATERAL(4,1)\|MICROBIAL CATION EXCHANGER(4,1)\|MINERAL ADJUVANT(4,1)\|NONPROFIT ORGANIZATION(4,1)\|NUTRIENT AVAILABILITY(4,1)\|OCEAN ACIDIFICATION(4,1)\|PELLET DISSOLUTION(4,1)\|PHOSPHATE ZINC PRECIPITATE(4,1)\|PHOSPHORUS ECOSYSTEM LOSS(4,1)\|PREAPPLICATION SOIL(4,1)\|PROGRESS FRACTIONATION(4,1)\|PROTONATED MICROBE(4,1)\|PULVERIZED LIMESTONE(4,1)\|PULVERIZED MG2SIO(4,1)\|QUASI GOVERNMENTAL REGULATOR(4,1)\|RENOWNED CHEMIST(4,1)\|RESERVOIR GEOLOGY(4,1)\|REWET BIOMASS(4,1)\|RIGOROUS COMPLIANCE(4,1)\|SOIL AMENDMENT AGRONOMIC PERFORMANCE(4,1)\|SOIL CULTIVATED ZONE(4,1)\|SOIL GEOCHEMISTRY(4,1)\|SOIL HYDROLOGY(4,1)\|SOIL STERILIZATION(4,1)\|SPECIALIZED TOOL(4,1)\|STEAM STERILIZATION(4,1)\|STYRENE DIVINYLBENZENE(4,1)\|TECHNO ECONOMIC MODELING(4,1)\|ULTIMATE PRICE(4,1)\|UREY REACTION BASIC PREMISE(4,1)\|VERIFICATION VERSION(4,1)\|VERIFIED ENHANCED ROCK(4,1)\|VOLUNTARY MARKET(4,1)\|X RAY FLUORESCENCE SPECTROSCOPY(4,1)\|CARBON DIOXIDE REMOVAL(3,10)\|AQUEOUS CO2(3,2)\|AVOIDED EMISSION(3,2)\|CARBONATE SPECIES(3,2)\|DISSOLVED CARBONATE(3,2)\|ENGINEERED MINERAL PRODUCT MODIFICATION(3,2)\|MARKET ABILITY(3,2)\|SECURE VESSEL(3,2)\|SOIL ENVIRONMENT(3,2)\|ABUNDANT CO2(3,1)\|ACCELERATE TIMING(3,1)\|ACTIVE BIOLOGICAL ABSORPTION PATHWAY(3,1)\|AGRONOMIC PERFORMANCE ENHANCEMENT(3,1)\|AQUEOUS BICARBONATE MEASUREMENT(3,1)\|AQUEOUS COMPLEXATION(3,1)\|ASBESTOS EXPOSURE(3,1)\|ASSEMBLING MP(3,1)\|ATTENDANT DEMAND(3,1)\|AUXILIARY GEOCHEMICAL DATA(3,1)\|BICARBONATE MOLE(3,1)\|BROAD FRAMEWORK(3,1)\|CARBON EXCHANGE TRANSACTION(3,1)\|CARBON VERIFICATION BENEFIT(3,1)\|COARSE PARTICLE(3,1)\|COLLECT CELL PELLET(3,1)\|CONTINENTAL COLLISION RELEASE(3,1)\|CROP HEALTH(3,1)\|DISSOLUTION ENHANCING(3,1)\|DIVALENT MG(3,1)\|EQUILIBRIUM EQUATION(3,1)\|FERTILIZATION FREQUENCY(3,1)\|FRAUDULENT SAMPLE(3,1)\|GROUND NATURAL ENVIRONMENT(3,1)\|H2CO SUM(3,1)\|INCREASE ECOSYSTEM COBENEFIT(3,1)\|LB BROTH(3,1)\|MINERAL TRANSFORMATION EXTENT(3,1)\|MINUS PROTON DONOR(3,1)\|PHOSPHATE LEACHING(3,1)\|PHOSPHATE MOBILITY(3,1)\|PRECISE ANSWER(3,1)\|PREEQUILIBRATED TUBE(3,1)\|REACTION THERMODYNAMICS(3,1)\|SECURITIZED CARBON REMOVAL(3,1)\|SILICATE MINERAL SHELL(3,1)\|SILICATE ROLE(3,1)\|UNSEALING SAMPLE(3,1)\|VERIFIABLE CARBON REMOVAL(3,1)\|XRF ANALYSIS(3,1)\|ANALYTICAL CHEMISTRY(2,3)\|LYSE(2,3)\|VSOIT(2,3)\|BAG(2,2)\|CO2 REMOVAL(2,2)\|FARMER(2,2)\|PELLETIZING(2,2)\|PRODUCT FORMULATION(2,2)\|STAKEHOLDER(2,2)\|TOTAL FORMULATION(2,2)\|ABILITY THRESHOLD(2,1)\|ACCEPTANCE(2,1)\|ACCOUNTING(2,1)\|ACID TREATED ARTHROBACTER(2,1)\|ACIDIC ENVIRONMENT(2,1)\|ACIDIC SOIL SOLUTION(2,1)\|ADDITIONALITY(2,1)\|ADMIXTURE(2,1)\|AERATION(2,1)\|AGLIME MESH SIZE OBSERVATION(2,1)\|AGRICULTURE(2,1)\|ALGAL BLOOM(2,1)\|ANALYTICAL PERFORMANCE(2,1)\|ANALYTICAL SOLUTION(2,1)\|APPLIED MINERAL AGRONOMIC BENEFIT(2,1)\|ATTRACTION(2,1)\|AUTOCLAVE(2,1)\|BACTERIA(2,1)\|BIOADSORBED METAL ACTIVE RELEASE(2,1)\|BIOFUEL(2,1)\|CA BEARING SILICATE(2,1)\|CA CONTENT(2,1)\|CALIBRATION STANDARD(2,1)\|CAPTURING CARBON(2,1)\|CARBON DIOXIDE FRACTIONAL PROGRESS(2,1)\|CARBON MARKET MATURATION(2,1)\|CARBON REMOVAL VERIFICATION(2,1)\|CARBON TRANSACTION(2,1)\|CATION EXCHANGE COLUMN(2,1)\|CHARGE BALANCE(2,1)\|CHELATOR(2,1)\|CHITOSAN(2,1)\|CLASSIFICATION(2,1)\|COMPUTING INDEX(2,1)\|CORTEVA CARBON(2,1)\|DRIED PELLET(2,1)\|EMPLACEMENT LOCATION(2,1)\|ENTIRE US ECONOMY(2,1)\|EXCHANGE COEFFICIENT(2,1)\|EXCHANGING RESIN(2,1)\|EXPERIMENTAL WORK(2,1)\|EXTANT FARM EQUIPMENT(2,1)\|FILTRATE ANALYSIS(2,1)\|FULL SUMMATION(2,1)\|GRIND CELL(2,1)\|HEAVY PHOSPHATE(2,1)\|ICP ANALYSIS(2,1)\|IMMOBILIZATION(2,1)\|INDIGO CARBON(2,1)\|LABORATORY SETTING(2,1)\|MARINE SETTING(2,1)\|MINERAL DELIVERY(2,1)\|MINERAL DISSOLUTION RATE(2,1)\|MINERAL POTENTIAL(2,1)\|NATURAL ABUNDANCE CALCULATION(2,1)\|NATURAL SOILS(2,1)\|NEGATIVE EMISSION(2,1)\|PLANT DEMAND(2,1)\|PROJECT EVALUATION CRITERIA(2,1)\|RELEVANT ION(2,1)\|ROCK ELEMENTAL ANALYSIS(2,1)\|ROCK MATERIAL ACCELERATED WEATHERING(2,1)\|SAMPLING DENSITY(2,1)\|SHARP THRESHOLD(2,1)\|SOIL ELEMENTAL ANALYSIS(2,1)\|SUBSURFACE SOIL PORE WATER(2,1)\|TECHNOLOGICAL SOLUTION(2,1)\|WET GRAM(2,1)\|	(EP4256520)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising:\| measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and\| subsequently measuring the immobile trace elements in a soil sample after application of the mineral amendment to verify application of the mineral amendment,\| characterized in that the method comprises the steps of:\| determining the amount of the mineral amendment added to the soil sample,\| determining the amount of measured divalent cations in the soil sample,\| determining the fractional carbon dioxide removal by comparing the applied divalent cations to the measured divalent cations in the soil sample.\|2. The method of claim 1, wherein the immobile trace elements and magnesium are measured using inductively coupled plasma spectroscopy or x-ray fluorescence spectroscopy.\|3. The method of claim 1, further comprising the step of measuring the immobile trace elements in the soil sample prior to addition of the mineral amendment.\|4. The method of claim 1, further comprising the step of enriching the abundance of the immobile trace elements in the mineral amendment.\|5. The method of claim 1, wherein: the rare earth elements comprise scandium (Sc), yttrium (Y), lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm), europium (Eu), gadolinium (Gd), terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), and lutetium (Lu); the rare metals comprise beryllium (Be), cesium (Cs), gallium (Ga), germanium (Ge), hafnium (Hf), niobium (Nb), rubidium (Rb), tantalum (Ta), titanium (Ti), vanadium (V), and zirconium (Zr); and the transition metals comprise nickel (Ni), chromium (Cr), and zinc (Zn).\|6. The method of claim 1 wherein three immobile trace elements are measured.\|7. The method of claim 6, wherein the three immobile trace elements are selected from the list comprising: (Y', 'La', 'Ce'), (Y', 'La', 'Pr'), (Y', 'La', Nd'), (Y', 'La', 'Sm'), (Y', 'La', 'Eh'), (Y', 'La', 'Gd'), (Y', 'La', 'Tb'), (Y', 'La', 'Dy'), (Y', 'La', 'Ho'), (Y', 'La', 'Er'), (Y', 'La', 'Tm'), ('Y', 'La', 'Yb'), ('Y', 'La', 'Lu'), (Y', 'Ce', 'Pr'), (Y', 'Ce', 'Nd'), (Y', 'Ce', 'Sm'), ('Y', 'Ce', 'Eh'), (Y', 'Ce', 'Gd'), (Y', 'Ce', 'Tb'), (Y', 'Ce', 'Dy'), (Y', 'Ce', 'Ho'), (Y', 'Ce', 'Er'), (Y', 'Ce', 'Tm'), (Y', 'Ce', 'Yb'), (Y', 'Ce', 'Eh'), ('Y', 'Pr', 'Nd'), (Y', 'Pr', 'Sm'), (Y', 'Pr', 'Eu'), (Y', 'Pr', 'Gd'), (Y', 'Pr', 'Tb'), (Y', 'Pr', 'Dy'), (Y', 'Pr', 'Ho'), ('Y', 'Pr', 'Er'), ('Y', 'Pr', 'Tm'), ('Y', 'Pr', Yb'), ('Y', 'Pr', 'Eh'), (Y', Nd', 'Sm'), (Y', d', 'Eh'), (Y', Nd', 'Gd'), (Y', Nd', 'Tb'), (Y', Nd', Dy'), (Y', Nd', 'Ho'), (Y', Nd', 'Er'), (Y', Nd', 'Tm'), (Y', Nd', Yb'), (Y', Nd', 'Lu'), (Y', 'Sm', 'Eu'), (Y', 'Sm', 'Gd'), (Y', 'Sm', 'Tb'), (Y', 'Sm', 'Dy'), (Y', 'Sm', 'Ho'), ('Y', 'Sm', 'Er'), (Y', 'Sm', 'Tm'), (Y', 'Sm', Yb'), (Y, 'Sm', 'Lu'), (Y', 'Eu', 'Gd'), ('Y', 'Eu', 'Tb'), (Y', 'Eu', 'Dy'), (Y, 'Eu', 'Ho'), (Y', 'Eu', 'Er'), ('Y', 'Eu', 'Tm'), (Y', 'Eu', Yb'), ('Y', 'Eu', 'Lu'), (Y', 'Gd', 'Tb'), ('Y', Gd', 'Dy'), (Y', Gd', 'Ho'), (Y', 'Gd', 'Er'), (Y', 'Gd', 'Tm'), (Y, 'Gd', Yb'), (Y, 'Gd', 'Lu'), (Y', 'Tb', 'Dy'), (Y', 'Tb', 'Ho'), (Y', 'Tb', 'Er'), (Y', 'Tb', 'Tm'), (Y, 'Tb', Yb'), (Y', 'Tb', 'Lu'), (Y', 'Dy', 'Ho'), (Y', 'Dy', 'Er'), (Y, 'Dy', 'Tm'), (Y, 'Dy', Yb'), ('Y', Dy', 'Lu'), ('Y', 'Ho', 'Er'), (Y', 'Ho', 'Tm'), (Y', 'Ho', Yb'), (Y', 'Ho', 'Lu'), ('Y', 'Er', 'Tm'), (Y', 'Er', Yb'), (Y', 'Er', 'Lu'), (Y', 'Tm', Yb'), ('Y', 'Tm', 'Lu'), (Y', Yb', 'Lu'), ('La', 'Ce', 'Pr'), ('La', 'Ce', Nd'), ('La', 'Ce', 'Sm'), ('La', 'Ce', 'Eu'), ('La', 'Ce', 'Gd'), ('La', 'Ce', 'Tb'), ('La', 'Ce', Dy'), ('La', 'Ce', 'Ho'), ('La', 'Ce', 'Er'), ('La', 'Ce', 'Tm'), ('La', 'Ce', Yb'), ('La', 'Ce', 'Lu'), ('La', 'Pr', Nd'), ('La', 'Pr', 'Sm'), ('La', 'Pr', 'Eu'), ('La', 'Pr', Gd'), ('La', 'Pr', 'Tb'), ('La', 'Pr', 'Dy'), ('La', 'Pr', 'Ho'), ('La', 'Pr', 'Er'), ('La', 'Pr', 'Tm'), ('La', 'Pr', Yb'), ('La', 'Pr', 'Lu'), ('La', Nd', 'Sm'), ('La', Nd', 'Eu'), ('La', Nd', 'Gd'), ('La', Nd', 'Tb'), ('La', Nd', 'Dy'), ('La', Nd', 'Ho'), ('La', Nd', 'Er'), ('La', Nd', 'Tm'), ('La', Nd', Yb'), ('La', Nd', 'Lu'), ('La', 'Sm', 'Eu'), ('La', 'Sm', 'Gd'), ('La', 'Sm', 'Tb'), ('La', 'Sm', 'Dy'), ('La', 'Sm', 'Ho'), ('La', 'Sm', 'Er'), ('La', 'Sm', 'Tm'), ('La', 'Sm', Yb'), ('La', 'Sm', 'Lu'), ('La', 'Eu', Gd'), ('La', 'Eu', 'Tb'), ('La', 'Eu', Dy'), ('La', 'Eu', 'Ho'), ('La', 'Eu', 'Er'), ('La', 'Eu', 'Tm'), ('La', 'Eu', Yb'), ('La', 'Eu', 'Lu'), ('La', 'Gd', 'Tb'), ('La', 'Gd', 'Dy'), ('La', 'Gd', 'Ho'), ('La', 'Gd', 'Er'), ('La', 'Gd', 'Tm'), ('La', Gd', Yb'), ('La', Gd', 'Lu'), ('La', 'Tb', 'Dy'), ('La', 'Tb', 'Ho'), ('La', 'Tb', 'Er'), ('La', 'Tb', 'Tm'), ('La', 'Tb', Yb'), ('La', 'Tb', 'Lu'), ('La', 'Dy', 'Ho'), ('La', 'Dy', 'Er'), ('La', 'Dy', 'Tm'), ('La', Dy', Yb'), ('La', Dy', 'Lu'), ('La', 'Ho', 'Er'), ('La', 'Ho', 'Tm'), ('La', 'Ho', Yb'), ('La', 'Ho', 'Lu'), ('La', 'Er', 'Tm'), ('La', 'Er', Yb'), ('La', 'Er', 'Lu'), ('La', 'Tm', Yb'), ('La', 'Tm', 'Lu'), ('La', Yb', 'Lu'), ('Ce', 'Pr', Nd'), ('Ce', 'Pr', 'Sm'), ('Ce', 'Pr', 'Eu'), ('Ce', 'Pr', 'Gd'), ('Ce', 'Pr', 'Tb'), ('Ce', 'Pr', 'Dy'), ('Ce', 'Pr', 'Ho'), ('Ce', 'Pr', 'Er'), ('Ce', 'Pr', 'Tm'), ('Ce', 'Pr', Yb'), ('Ce', 'Pr', 'Lu'), ('Ce', Nd', 'Sm'), ('Ce', Nd', 'Eu'), ('Ce', Nd', Gd'), ('Ce', Nd', 'Tb'), ('Ce', Nd', 'Dy'), ('Ce', Nd', 'Ho'), ('Ce', Nd', 'Er'), ('Ce', Nd', 'Tm'), ('Ce', Nd', Yb'), ('Ce', Nd', 'Lu'), ('Ce', 'Sm', 'Eu'), ('Ce', 'Sm', 'Gd'), ('Ce', 'Sm', 'Tb'), ('Ce', 'Sm', 'Dy'), ('Ce', 'Sm', 'Ho'), ('Ce', 'Sm', 'Er'), ('Ce', 'Sm', Tm'), ('Ce', 'Sm', 'Yb'), ('Ce', 'Sm', 'Lu'), ('Ce', 'Eu', 'Gd'), ('Ce', 'Eii', Tb'), ('Ce', 'Eu', 'Dy'), ('Ce', 'Eu', 'Ho'), ('Ce', 'Eu', 'Er'), ('Ce', 'Eu', 'Tm'), ('Ce', 'Eu', Yb'), ('Ce', 'Eu', 'Lu'), ('Ce', 'Gd', 'Tb'), ('Ce', 'Gd', 'Dy'), ('Ce', Gd', 'Ho'), ('Ce', 'Gd', 'Er'), ('Ce', 'Gd', 'Tm'), ('Ce', 'Gd', Yb'), ('Ce', 'Gd', 'Lu'), ('Ce', 'Tb', 'Dy'), ('Ce', 'Tb', 'Ho'), ('Ce', 'Tb', 'Er'), ('Ce', 'Tb', 'Tm'), ('Ce', 'Tb', Yb'), ('Ce', 'Tb', 'Lu'), ('Ce', 'Dy', 'Ho'), ('Ce', Dy', 'Er'), ('Ce', 'Dy', 'Tm'), ('Ce', 'Dy', Yb'), ('Ce', 'Dy', 'Lu'), ('Ce', 'Ho', 'Er'), ('Ce', 'Ho', 'Tm'), ('Ce', 'Ho', Yb'), ('Ce', 'Ho', 'Lu'), ('Ce', 'Er', 'Tm'), ('Ce', 'Er', Yb'), ('Ce', 'Er', 'Lu'), ('Ce', 'Tm', Yb'), ('Ce', 'Tm', 'Lu'), ('Ce', Yb', 'Lu'), ('Pr', 'Nd', 'Sm'), ('Pr', 'Nd', 'Eu'), ('Pr', 'Nd', Gd'), ('Pr', 'Nd', 'Tb'), ('Pr', 'Nd', Dy'), ('Pr', 'Nd', 'Ho'), ('Pr', Yd', 'Er'), ('Pr', Yd', 'Tm'), ('Pr', Yd', Yb'), ('Pr', Yd', 'Lu'), ('Pr', 'Sm', 'Eu'), ('Pr', 'Sm', 'Gd'), ('Pr', 'Sm', 'Tb'), ('Pr', 'Sm', Dy'), ('Pr', 'Sm', 'Ho'), ('Pr', 'Sm', 'Er'), ('Pr', 'Sm', 'Tm'), ('Pr', 'Sm', Yb'), ('Pr', 'Sm', 'Lu'), ('Pr', 'Eu', Gd'), ('Pr', 'Eu', 'Tb'), ('Pr', 'Eu', 'Dy'), ('Pr', 'Eu', 'Ho'), ('Pr', 'Eu', 'Er'), ('Pr', 'Eu', 'Tm'), ('Pr', 'Eu', Yb'), ('Pr', 'Eu', 'Lu'), ('Pr', Gd', 'Tb'), ('Pr', 'Gd', Dy'), ('Pr', 'Gd', 'Ho'), ('Pr', 'Gd', 'Er'), ('Pr', 'Gd', 'Tm'), ('Pr', 'Gd', Yb'), ('Pr', 'Gd', 'Lu'), ('Pr', 'Tb', 'Dy'), ('Pr', 'Tb', 'Ho'), ('Pr', 'Tb', 'Er'), ('Pr', 'Tb', 'Tm'), ('Pr', 'Tb', Yb'), ('Pr', 'Tb', 'Lu'), ('Pr', 'Dy', 'Ho'), ('Pr', 'Dy', 'Er'), ('Pr', Dy', 'Tm'), ('Pr', Dy', Yb'), ('Pr', 'Dy', 'Lu'), ('Pr', 'Ho', 'Er'), ('Pr', 'Ho', 'Tm'), ('Pr', 'Ho', Yb'), ('Pr', 'Ho', 'Lu'), ('Pr', 'Er', 'Tm'), ('Pr', 'Er', Yb'), ('Pr', 'Er', 'Lu'), ('Pr', 'Tm', Yb'), ('Pr', 'Tm', 'Lu'), ('Pr', Yb', 'Lu'), (Yd', 'Sm', 'Eu'), (Yd', 'Sm', 'Gd'), (Yd', 'Sm', 'Tb'), (Yd', 'Sm', 'Dy'), (Yd', 'Sm', 'Ho'), (Yd', 'Sm', 'Er'), (Yd', 'Sm', 'Tm'), (Yd', 'Sm', Yb'), (Yd', 'Sm', 'Lu'), (Yd', 'Eu', 'Gd'), (Yd', 'Eu', 'Tb'), (Yd', 'Eu', 'Dy'), (Yd', 'Eu', 'Ho'), (Yd', 'Eu', 'Er'), (Yd', 'Eu', 'Tm'), (Yd', 'Eu', Yb'), (Yd', 'Eu', 'Lu'), (Yd', 'Gd', 'Tb'), (Yd', 'Gd', 'Dy'), (Yd', Gd', 'Ho'), (Yd', 'Gd', 'Er'), (Yd', 'Gd', 'Tm'), (Yd', 'Gd', Yb'), (Yd', 'Gd', 'Lu'), (Yd', 'Tb', Dy'), (Yd', 'Tb', 'Ho'), (Yd', 'Tb', 'Er'), (Yd', 'Tb', 'Tm'), (Yd', 'Tb', Yb'), (Yd', 'Tb', 'Lu'), (Yd', 'Dy', 'Ho'), (Yd', 'Dy', 'Er'), (Yd', 'Dy', 'Tm'), (Yd', 'Dy', Yb'), (Yd', 'Dy', 'Lu'), (Yd', 'Ho', 'Er'), (Yd', 'Ho', 'Tm'), (Yd', 'Ho', Yb'), (Yd', 'Ho', 'Lu'), (Yd', 'Er', 'Tm'), (Yd', 'Er', Yb'), (Yd', 'Er', 'Lu'), (Yd', 'Tm', Yb'), (Yd', 'Tm', 'Lu'), (Yd', Yb', 'Lu'), ('Sm', 'Eu', 'Gd'), ('Sm', 'Eu', 'Tb'), ('Sm', 'Eu', 'Dy'), ('Sm', 'Eu', 'Ho'), ('Sm', 'Eu', 'Er'), ('Sm', 'Eu', 'Tm'), ('Sm', 'Eu', Yb'), ('Sm', 'Eu', 'Lu'), ('Sm', 'Gd', 'Tb'), ('Sm', 'Gd', 'Dy'), ('Sm', 'Gd', 'Ho'), ('Sm', 'Gd', 'Er'), ('Sm', 'Gd', 'Tm'), ('Sm', 'Gd', Yb'), ('Sm', 'Gd', 'Lu'), ('Sm', 'Tb', 'Dy'), ('Sm', 'Tb', 'Ho'), ('Sm', 'Tb', 'Er'), ('Sm', 'Tb', 'Tm'), ('Sm', 'Tb', Yb'), ('Sm', 'Tb', 'Lu'), ('Sm', Dy', 'Ho'), ('Sm', 'Dy', 'Er'), ('Sm', Dy', 'Tm'), ('Sm', 'Dy', Yb'), ('Sm', Dy', 'Lu'), ('Sm', 'Ho', 'Er'), ('Sm', 'Ho', 'Tm'), ('Sm', 'Ho', Yb'), ('Sm', 'Ho', 'Lu'), ('Sm', 'Er', 'Tm'), ('Sm', 'Er', Yb'), ('Sm', 'Er', 'Lu'), ('Sm', 'Tm', Yb'), ('Sm', 'Tm', 'Lu'), ('Sm', Yb', 'Lu'), ('Eu', 'Gd', 'Tb'), ('Eu', 'Gd', 'Dy'), ('Eu', 'Gd', 'Ho'), ('Eu', 'Gd', 'Er'), ('Eu', 'Gd', 'Tm'), ('Eu', 'Gd', Yb'), ('Eu', 'Gd', 'Lu'), ('Eu', 'Tb', 'Dy'), ('Eu', 'Tb', 'Ho'), ('Eu', 'Tb', 'Er'), ('Eu', 'Tb', 'Tm'), ('Eu', 'Tb', Yb'), ('Eu', 'Tb', 'Lu'), ('Eu', 'Dy', 'Ho'), ('Eu', 'Dy', 'Er'), ('Eu', Dy', 'Tm'), ('Eu', Dy', Yb'), ('Eu', Dy', 'Lu'), ('Eu', 'Ho', 'Er'), ('Eu', 'Ho', 'Tm'), ('Eu', 'Ho', Yb'), ('Eu', 'Ho', 'Lu'), ('Eu', 'Er', 'Tm'), ('Eu', 'Er', Yb'), ('Eu', 'Er', 'Lu'), ('Eu', 'Tm', Yb'), ('Eu', 'Tm', 'Lu'), ('Eu', Yb', 'Lu'), ('Gd', 'Tb', Dy'), ('Gd', 'Tb', 'Ho'), ('Gd', 'Tb', 'Er'), ('Gd', 'Tb', 'Tm'), ('Gd', 'Tb', Yb'), ('Gd', 'Tb', 'Lu'), ('Gd', Dy', 'Ho'), ('Gd', 'Dy', 'Er'), ('Gd', 'Dy', 'Tm'), ('Gd', Dy', Yb'), ('GcT, 'Dy', 'Lu'), ('Gd', 'Ho', 'Er'), ('Gd', 'Ho', Tm1), (Gd', 'Ho', 'Yb'), ('Gd', 'Ho', 'Lu'), (Gd', 'Er', Tm'), ('Gd', 'Er', Yb'), ('Gd', 'Er', 'Lu'), ('Gd', 'Tm', Yb'), ('Gd', 'Tm', 'Lu'), ('Gd', Yb', 'Lu'), ('Tb', 'Dy', 'Ho'), ('Tb', 'Dy', 'Er'), ('Tb', 'Dy', 'Tm'), ('Tb', Dy', Yb'), ('Tb', 'Dy', 'Lu'), ('Tb', 'Ho', 'Er'), ('Tb', 'Ho', 'Tm'), ('Tb', 'Ho', Yb'), ('Tb', 'Ho', 'Lu'), ('Tb', 'Er', 'Tm'), ('Tb', 'Er', Yb'), ('Tb', 'Er', 'Lu'), ('Tb', 'Tm', Yb'), ('Tb', 'Tm', 'Lu'), ('Tb', Yb', 'Lu'), ('Dy', 'Ho', 'Er'), ('Dy', 'Ho', 'Tm'), ('Dy', 'Ho', Yb'), ('Dy', 'Ho', 'Lu'), ('Dy', 'Er', 'Tm'), ('Dy', 'Er', Yb'), ('Dy', 'Er', 'Lu'), ('Dy', 'Tm', Yb'), ('Dy', 'Tm', 'Lu'), ('Dy', Yb', 'Lu'), (Ho', 'Er', 'Tm'), (Ho', 'Er', Yb'), (Ho', 'Er', 'Lu'), (Ho', 'Tm', Yb'), (Ho', 'Tm', 'Lu'), (Ho', Yb', 'Lu'), ('Er', 'Tm', Yb'), ('Er', 'Tm', 'Lu'), ('Er', Yb', 'Lu'), and ('Tm', Yb', 'Lu').\|8. The method of claim 1, wherein the step of measuring the immobile trace elements in a soil sample after application of the mineral amendment further comprises lysing the soil sample and application of ethylenediaminetetraacetic acid.	(EP4256520)\|Cross Reference to Related Applications\|[0001] The present applications claims the priority benefit of U.S. Provisional Patent App. Serial No. 63/322,672, filed March 23, 2022; U.S. Provisional Patent App. Serial No. 63/289,395, filed December 14, 2021; and U.S. Provisional Patent App. Serial No. 63/213,398, filed, June 22, 2021.\|Background\|[0002] The last several years have witnessed a maturation of carbon markets from lightly scrutinized voluntary markets largely serving to provide positive marketing collateral to familiar consumer brands to rigorous compliance markets with proof-of-performance requirements often involving government and quasi-governmental regulators. There have also been a number of comprehensive proposals for decarbonization of the entire US economy, combining energy production, transportation, cement production, and agriculture. These proposals have included carbon dioxide removal (CDR) techniques as an essential component of the decarbonization plan, with a supportive ecosystem of science, policy, and project evaluation criteria. Within the diverse scope of decarbonization efforts, including renewable energy, biofuel, nature-based solutions, and more technical CDR techniques like direct air capture (DAC), The Oxford Principles have developed a taxonomy for categorizing diverse decarbonization strategies. This taxonomy distinguishes between avoided emissions (for instance, conversion of fossil fuel power to renewable power) and negative emissions (for instance direct air capture); distinguishes between avoided emissions that require storage (for instance carbon capture from a point source and sequestration into the ground) and those that do not require storage (the conversion to renewable energy); and the duration of the storage if so required (for instance, short lived forest carbon sequestration from delayed harvests versus storage of captured carbon in geological formations).\|[0003] A number of for-profit and non-profit organizations have emerged that employ the Oxford Principles to evaluate proposals, particularly around the rigorous quantification across categories (Table 1). This, in essence, is the scorecard that projects will have to compete on to find acceptance in the industry. All other things equal, cost ends up being the primary driver, but quality is also a key consideration. Thus, historically buyers have been drawn to nature-based solutions that cost between $5-20/tCO2 e (e.g., Corteva Carbon, Indigo Carbon), versus direct air capture projects that cost >$500/tCO2 e (e.g., ClimeWorks). However, there are challenges to these nature-based solutions: recently these nature-based solutions have been subject to intense scrutiny for "gaming" the rules or otherwise failing to deliver prospective rewards. Among the technological solutions, there are a different set of challenges: rigor has been strong, but the reduction in price proportional to increase in deployment has been slow, and the ultimate price of DAC is not expected to drop below $150/tCO2e (Keith et al 2018, https://doi.org/10.1016/j.joule.2018.05.006). In light of these challenges, we have developed a technology around "enhanced rock weathering" (ERW), in which silicate minerals are weathered in acidic soil solution, thus driving the uptake of additional CO2 into dissolved inorganic carbon (DIC) in the soil solution. Our experimental work, life cycle analysis, and techno-economic modeling have indicated that ERW provides the permanence, additionality, and rigorous quantification of a DAC project, the large volume of a carbon capture and storage (CCS) project, and the unit economics of a nature based solution, thus creating a new tool to meet net-zero goals.\|Details of Enhanced Rock Weathering\|[0004] In "enhanced rock weathering" (ERW), silicate minerals are weathered by CO2 from the ambient air which has been dissolved into water, reacting to produce dissolved inorganic carbon that is ultimately stored in the ocean as depicted in FIGS. 1 and 2.\|Background Geochemistry\|[0005] The role of silicate rock weathering in maintaining the CO2 balance of the atmosphere has been recognized for decades, first outlined by renowned chemist Harold Urey in the 1950s. The basic premise of the Urey reaction is that continental collisions release CO2 to the atmosphere from volcanoes, and bring Mg- and Ca-bearing silicate rocks to the surface. The rainwater (H2O) that falls upon these rocks is mildly acidic, as atmospheric CO2 has dissolved in it and formed carbonic acid (H2CO3). For forsterite, the weathering reaction takes place following the form:\| Mg2SiO4 + 4 H2O + 4 CO2 → 2 Mg2+ + 4 HCO3- + 4 H4SiO4\|[0006] In this reaction, one mole of forsterite consumes four moles of CO2, so two negatively charged bicarbonate HCO3- are created for every one divalent Mg2+ weathered. Given the molecular weight of forsterite (140 g/mol) and the molecular weight of CO2 (44 g/mol), weathering one metric ton of forsterite removes 1.25 metric tons of CO2 from the atmosphere. In general, such a formula can be used to define the "mineral potential" of a silicate based on its elemental composition: \| where V is the valence of the cation (2 for Mg and Ca) and MW is the molecular weight.\|[0007] The rate of weathering is determined by the surface area of the mineral, the acidity (pH) of the soil solution, the temperature of the solution, the availability of CO2 reagent in solution, and the rate of removal of the reaction products by water. One of the key insights into the potential of "enhanced" rock weathering is that the rate of reaction, and thus CO2 removal, can be greatly accelerated by increasing the surface area by pulverization into a fine powder (e.g., less than 100 um), incorporating into an acidic environment (e.g., pH less than 6) with abundant CO2 present, and with steady water flux to remove reaction products to maintain acidity. While this formula defines the potential amount of CO2 that may be removed by weathering, it does not speak to the rate; ancient rock formations testify that the rate of weathering can be extremely slow.\|[0008] The relationship between silicates (like Mg2SiO4) and dissolved carbonates (like HCO3-) is not necessarily intuitive, as the carbonate system of water involves a number of coupled reactions. Atmospheric CO2 dissolves into water according to an exchange coefficient:\| CO2(aq) = H2CO3 = KCO2 * pCO2\|[0009] Technically pCO2 is "fugacity" that represents its activity, but, as used herein, it is more or less equivalent to its partial pressure, and KCO2 is the Henry's law coefficient that determines the aqueous CO2 in equilibrium with the atmosphere. This aqueous CO2 in turn hydrates with H2O to become carbonic acid (H2CO3), which dissociates to become bicarbonate (HCO3-) and carbonate (CO32-):\| H2CO3 ↔ HCO3- + H+\| HCO3- ↔ CO32- + H+\|[0010] These equilibrium reactions are defined by K1 and K2, the first and second carbonate system dissociation constants. pK1 and pK2 are about 5.9 and about 9.4 at STP, so greater than 99% of the charge in the dissolved carbonates is HCO3-.\|[0011] The carbonates are the largest constituents of total alkalinity, which is defined as the charge imbalance between weak acids (proton acceptors) minus proton donors:\| TA = [HCO3-] + 2 · [CO32-] + [OH-] - [H+]\|[0012] There is an alternative definition of total alkalinity as the charge imbalance between conserved cations and conserved anions:\| TA = [Na+] + 2 [Mg2+] + 2 [Ca2+] + [K+] + ... - [Cl-] - 2 [SO42-] - [NO3-]\|[0013] These two expressions are always equal (i.e. the charges balance). This means that an added Mg or Ca into soil solution will increase in HCO3- to balance the charge. We describe an analytical solution to compute how much carbon is taken up per unit of additional Mg or Ca. If we first define DIC as the sum of H2CO3, HCO3-, and CO32-, and make use of the equilibrium equations above (defining H+ as "h" and H2CO3 as "s"): \|[0014] And formulate TA using the same convention: \|[0015] With these definitions in place, we can develop an estimate of dDIC/dTA. First, we compute the derivative dTA/dh: \|[0016] Next we compute the derivative dDIC/dh: \|[0017] Finally we multiply dDIC/dh by the inverse of dTA/dh to calculate dDIC/dTA: \|[0018] At the pH found in soils, each Mg or Ca is matched by two carbon atoms. In all circumstances, raising alkalinity results in increased pH. This is particularly important in marine settings, where ocean acidification from increased atmospheric CO2 can be ameliorated by this export of alkalinity from land.\|[0019] The potential for ERW as a commercial enterprise is limited by some fundamental issues:\| A. The total amounts of mineral transformation and carbon removal should be verifiable empirically. The verification methods described below may be low cost at scale, can be performed at arm's length by a 3rd party, and may have safeguards to eliminate fraud.\|[0020] Additionally, the commercial potential for ERW could be enhanced by a number of different features. Embodiments may include:\| B. Processes and modifications of the engineered mineral product that enhance the agronomic performance and ecosystem co-benefits of the engineered mineral.\| C. Processes and modifications of the engineered mineral product that control or enhance the mineral dissolution rate of the engineered mineral in soil environments and thus the rate of removal of CO2.\| C. Paulo et al, Applied Geochemistry, 2021, 219, 104955, discusses evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralisation.\| N. Moosdorf et al, Environ. Sci. Tech., 2014, 48, 4809 discusses carbon dioxide efficiency of terrestrial enhanced weathering and determination of effective carbon dioxide sequestration.\|Brief Description of the Drawings\|[0021] FIG. 1 is a drawing illustrating the enhanced rock weathering cycle.\| FIG. 2 is a graph depicting the effect of comminution on dissolution kinetics for a silicate.\| FIGS. 3A to 3D are graphs depicting the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um which closely approximates the alkalinity release dynamics for aglime.\| FIG. 4 is a drawing illustrating the general scheme for a verified enhanced rock weathering cycle.\|Detailed Description\|[0022] Summary: The following described methodologies can establish one version of a verification scheme that will demonstrate the transformation of the applied rock material and the subsequent carbon removal into secure geologic reservoirs as evidenced by observations collected from the soil. One set of methods (A) can measure the production of free ions from the applied material and the transport of those ions outside of a control volume as a direct measure of the amount of weathering and thus total carbon dioxide equivalent isolated from the atmosphere. Furthermore, as the elemental inputs into the soil induced by enhanced rock weathering can have significant effects on the soil geochemistry, methods in (B) describe systems and versions that can enhance the agronomic performance of the soil amendment and increase ecosystem co-benefits. Lastly, methods in (C) elaborate on versions that control and enhance the mineral dissolution rate, which increases the financial performance of enhanced rock weathering technology in the marketplace.\| A. Systems and methods for monitoring and verification:Described below are several example methodologies for quantifying the rate and extent of mineral transformation and carbon removal, which are referred to as "verification methodologies".1. Example Verification methodology 1:a. A cation exchange resin and/or an anion exchange resin are packaged into a physical embodiment (such as a 5 cm diameter tube, 5cm in length, placed 30 cm below the soil surface) that allows vertical transport of fluids but not horizontal transport.\| b. Commercial ion exchange resins are pre-equilibrated in such a way that their selectivity is high for the relevant ions, but their capacity is also sufficiently high such that saturation is minimized. This technology may allow for effective deployment for long periods of time, allowing passage of up to 4000 mm of moisture through the tube, without becoming saturated with respect to the ions of interest.\| c. The ions of interest are restricted to divalent cations (Mg2+, Ca2+), carbonate species (HCO3- and CO32-), and silicic acid (H4SiO4), important weathering products of preferred mineral soil amendments, such as ultramafic rocks, blast furnace slag, and other naturally occurring or industrial silicate minerals with high Mg and Ca content.\| d. Three pre-equilibrated tubes are emplaced fully under the soil below a control depth (e.g., 30 cm, a typical depth of cultivation). This may be done by removing the top 30 cm soil with a shovel or auger, then gently placing the tube in the created void space. Following a certain period of time post-surface application of mineral soil amendment (e.g., 9 to 12 months after application), the tubes are retrieved, and the ions captured within the resin exchanges are measured using standard methodologies, such as ICP-OES and ICP-MS based concentration measurements. Three tubes are used to determine standard deviation error in triplicate.\| e. By the principle of charge balance and known thermodynamic reactions taking place in the top 30 cm of soils, the amount of carbonate can be inferred purely from the measurement of cations, under certain assumptions and auxiliary geochemical data. By the addition of more specific anion exchange resins, such as styrenedivinylbenzene, these assumptions can be avoided to get a more precise answer. The increase in cation concentration in the subsurface soil pore water allows for the stoichiometric determination of carbon removal from the gas phase (ambient air).\| f. The total carbon dioxide removed during the deployment period may be estimated as equal to the molecular mass of CO2 (44 g/mol) multiplied by the sum of the number of moles of carbonate and two times the number of moles of bicarbonate, multiplied by the area on which mineral was applied to the field, divided by the cross-sectional area of the tube.\| g. Direct measurement of aqueous bicarbonate and carbonate species, which are the most readily available forms of carbon induced by a gas exchange of carbon dioxide with the soil pore water, may be conducted using the specified anion exchange resin above. The expression as described in clause (f) explains the calculation used to convert this direct measurement of carbon to an absolute value of carbon dioxide removed during a specified application period.\| h. Verification methodology 1 has the advantage that it can provide a direct measure of carbon flux and employs a measurement technique that is mature.\| i. However, potential disadvantages may include the need for manufacturing (and its attendant demand for working capital); devices may occasionally be defective; emplacement of a device may alter the flow paths of water, which in turn alters the inferred ion fluxes; emplacement of a device may depend on the user; the knowledge of the location of emplacement may invite manipulation by a stakeholder involved in a carbon transaction; and others. 2. Example Verification methodology 2:a. The principle behind Verification methodology 2 is that minerals applied for purposes of enhanced rock weathering contain, in addition to the elements outlined above that participate in the weathering reaction (i.e., magnesium, calcium, iron, silicon, oxygen, hydrogen), additional elements in trace amounts. These additional trace elements (TEs) might include rare earth elements (REEs), rare metals (RM), other transition metals (TMs), or a combination thereof. Unlike the primary weathering products that are readily dissolved in solution and lost by leaching, some TEs are strongly bound to mineral and biological surfaces and do not readily leach from the soil control volume (e.g., the top 10 to 30 cm of soil), and are not removed by plants at the concentrations present in our applied rock. These strongly bound trace elements are referred to herein as immobile trace elements (ITEs). Thus, a measure of cumulative cation flux and carbon removal can be computed by comparing the ratio of the lost weathering products, such as magnesium, to ITEs, after accounting for background concentrations of ITEs in the initial soil.\| b. As used herein, rare earth elements include scandium (Sc), yttrium (Y), lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm), europium (Eu), gadolinium (Gd), terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), lutetium (Lu) or a combination thereof. As used herein, rare metals include beryllium (Be), cesium (Cs), gallium (Ga), germanium (Ge), hafnium (Hf), niobium (Nb), rubidium (Rb), tantalum (Ta), zirconium (Zr), or a combination thereof. As used herein, transition metals include nickel (Ni), chromium (Cr), and zinc (Zn) among others and may include a combination of transition metals.\| c. An approach based on ITEs depends on the degree of immobility of the element in soil environments, the time horizon after which the ITEs will be measured to estimate carbon removal, the abundance of ITEs in both the soil and the mineral added, and the analytical chemistry used to measure this abundance. An analytical technique that has low detectability thresholds for slightly mobile elements could be sufficient for relatively abundant (e.g., parts per thousand to parts per million) elements over short time horizons (e.g., weeks to months). On the other hand, a different analytical technique could be used over longer time horizons, which in turn could involve quantification of very immobile elements that are present in much lower abundance (e.g., parts per billion to parts per trillion). The approach may be chosen based at least in part on cost, which ITEs are actually conserved, over which time horizons, as well as the performance of the analytical performance used.\| d. The relative proportions of ITEs in a sample (rock or soil) constitute a type of unique fingerprint of the material. Because the cost of pure ITEs is large, and the analytical chemistry is not widely available, there is a significant barrier to engineering a fraudulent sample to reproduce the native ITE fingerprint of a mineral soil amendment. Thus, it would be challenging for a stakeholder in a carbon exchange transaction to generate a result that produces the anticipated result (a high or low amount of carbon removal) while also matching the ITE fingerprint generated by a bona fide sample. This is a contrast with measurement schemes for soil organic carbon, in which the landowner or other interested party has an information advantage in terms of where or when to sample, which could be used to achieve a particular carbon measurement objective (high or low).\| e. Verification Methodology 2 (VM2) has advantages over Verification Methodology 1 (VM1) in that it avoids the need for the use of a device, which avoids altering the soil hydrology or physical environment in a way that would impact the observed elemental analysis.\| f. VM2 may have an advantage over VM1 in not requiring tracking of a specific location for recovering the sampling column.\| g. VM2 does, however, include measurement techniques that are less widely available; requires specialized instruments and personnel; requires additional boundary conditions to compute carbon flux (e.g., pre-application soil and rock elemental analysis); and employs assumptions as to the relationship between cation flux and carbon flux.\| h. Like VM1, VM2 uses the total amount of mineral applied and the field area, which could be measured, for example, using a digital as-applied map commonly accompanying crops input machinery, or truck weights before and after mineral delivery. This will be referred to as the nominal application rate (ARnominal).\| i. There are four main calculations in VM2. To the extent any one of these factors is known unambiguously from other sources, each step in VM2 could be used in isolation from the others.i. Classify, using ITE fingerprinting, whether a soil has had a specific mineral applied, which may be asserted by an entity wishing to make a claim;\| ii. Calculate, using ITE fingerprinting, what the actual mineral application rate (ARactual) for a specific soil sample was, which will necessarily differ in a systematic or random way from the average rate for the entire field;\| iii. Calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the application rate in (ii) above;\| iv. Calculate, using the fraction computed in (iii) and the mineral potential (Equation 1) computed for the feedstock identified in (i) above, the amount of carbon dioxide removed. j. In one non-limiting embodiment, the verification methodology to classify whether the claimed mineral applied is the actual mineral applied is as follows:i. Collect a sample from mineral to be applied, place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Mineral Amendment.\| ii. Prior to mineral application, collect a 20 g sample from cultivated zone of soil (typically at around 30 cm, such as in a range of 0 cm to 30 cm), place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Soil A.\| iii. Subsequent to mineral application, collect a 20 g sample the same control zone as soil A, and store under similar conditions. Label as Soil B. Soil B could be sampled immediately after mineral application or at a later time (e.g., months to years afterwards).\| iv. Characterize the elemental composition of Mineral Amendment, Soil A, and Soil B. Example approaches to characterizing the elemental composition are described in (v) and (vi).\| v. One approach to measuring the elemental composition is as follows:1. In a laboratory setting, unseal the soil samples and place 10 grams of Soil A and Soil B in two separate beakers.\| 2. Dissolve the solids in strong acid. For example, add 21 mL of strong 1.0 M hydrochloric acid and 7 mL of strong 1.0 M nitric acid (total 28 mL acid) to each beaker of sterilized soil and stir rigorously until solids are dissolved.\| 3. Filter the sample-containing beakers first through a 1- to 5-micron water filter cartridge followed by an attached 10 to 20 cm column cation exchange resin at a sufficiently slow flow rate of, for example, 1 to 5 mL/min. This combination of a water filter with a cation exchange column has been engineered for optimal performance with soils under consideration. Specifically, the 5-micron water filter cartridge separates out any larger particles, allowing for the smaller particles to exchange its bound metals with the subsequent cation exchange resin.\| 4. Flush copious amounts (e.g., 100-200 mL) of 0.5 to 1.0 M chelator such as, for example, ethylenediaminetetraacetic acid (EDTA) at 1-5 mL/min through the used filters into their respective filtrates. This may collect any additional metals that were still adhered to the filters.\| 5. Send filtrate A (resultant sample from Soil A) and filtrate B (resultant sample from Soil B) to an analytical laboratory for analysis on an inductively coupled plasma mass spectrometer (ICP-MS). Measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3.\| 6. The ICP-MS may be set to detect magnesium concentrations and the following 17 elements on a high ppb or low ppm detection level: Yttrium, Scandium, Lanthanum, Cerium, Praseodymium, Neodymium, Promethium, Samarium, Europium, Gadolinium, Terbium, Dysprosium, Holmium, Erbium, Thulium, Ytterbium, Lutetium. Classify light rare earth elements (LREEs) as yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium. Classify heavy rare earth elements (HREEs) as europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium. Send an isolated rock material sample for ICP-MS analysis. Similar to the filtrate analyses, measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3. vi. Another approach to measuring the elemental composition is as follows:1. Calibrate a portable XRF instrument for particularly low detection limit of ITEs using a calibration standard (such as Bruker proprietary Geo calibration + custom ITE standards).\| 2. Use the portable XRF instrument to analyze the Rock Material and Soil A for ITEs (as identified in Verification methodology 2), reporting the instrumental error (2 standard deviations) as well.\| 3. Use the portable XRF instrument to analyze Soil B for ITEs, reporting the instrumental error (2 standard deviations) as well. vii. Once the above elemental composition has been determined, calculate the difference for every element between Mineral Amendment and Soil A, resulting in a vector of differences vrock. Likewise, compute the difference for every element between Soil B and Soil A, resulting in a vector of differences vsoil. To improve performance, each element may be divided by an individual factor, such as the detection threshold, or the instrumental uncertainty, or the elemental composition of a reference material. Another means to improve performance would be to sum a subset of the elements or several distinct subsets of elements before computing vrock and vsoil. Another means to improve performance would be to compute indices of these summed subsets of elements, for example the ratio of the light REEs to the heavy REEs, before computing vrock and vsoil.\| viii. Compute the dot product of vrock and vsoil. If the value of this dot product is close to 1 (e.g., within a threshold value), then the Soil B is positively classified as having the Mineral Amendment. If the value of the dot product is less than 1 minus a threshold value, then Soil B is negatively classified as not having the Mineral Amendment.\| ix. The threshold value may be determined using a variety of means, for example the half-angle between the dot product of vrock and vsoil and any other known vrock and vsoil; or using a Monte Carlo simulation of vrock and vsoil that accounts for known sources of uncertainty including instrumental error, variation in rock elemental analysis, or variation of soil elemental analysis. k. In one non-limiting embodiment, the verification methodology to calculate the actual mineral application rate (ARactual) for a specific soil sample is as follows:i. Characterize the elemental composition the elemental composition of Mineral Amendment, Soil A, and Soil B as above. Note that there could be different analytical chemistry employed if, for example, rapid and inexpensive XRF analysis was used for classification soon after application, and slower and more costly ICP analysis may be used to estimate application rates.\| ii. Compute the differences in elemental composition as above, potentially including similar performance enhancements such as normalizing by factors specific to each element, summing across subsets of elements, and computing indices such as the ratio of light REEs to heavy REEs. Such transformed and summed variables for a sample will be referred to generically as ΣITEsample.\| iii. The actual application rate of the sample can be calculated using the following expression: l. In one non-limiting embodiment, the verification methodology to calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the actual mineral application rate (ARactual) as follows:i. The amount of divalent cations applied (DCapplied) can be calculated by the proven identity of the mineral additive and the actual application rate: where divalent cations are generally restricted in this context to Mg and Ca, and Mgmineral and Camineral is the fractional composition of the mineral additive.\| ii. The amount of divalent cations remaining (DCremain) in the soil could be estimated using the same elemental analysis as previously (if, for example, ICP-MS was used), or determined from the same sample using a different analysis (if, for example XRF was used and Mg was not measured).\| iii. The fractional progress of carbon dioxide removal (CDR) can be estimated by the ratio of remaining divalent cations to applied divalent cations: m. In one non-limiting embodiment, the verification methodology to calculate the amount of carbon dioxide removed from the control volume is as follows:i. Assembling MP, fCDR , ARnominal and the land area applied, the total carbon dioxide removal is: n. While Verification Methodology 2 presented herein provides a broad framework for the detection and application of soil-bound ITEs to estimate long-term geologic carbon drawdown, the efficacy of the approach can also be improved through the focus on specific subsets of ITEs. Non-limiting embodiments of such improvements are listed below:i. The ITEs specified in equation 2, e.g., (ΣITEssoil B), may in fact be represented not by the full summation of 17 REEs but instead by the use of only LREEs or the use of only HREEs, as defined in clause xii. Such a calculation would mean the sum of only LREEs in the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium) or the sum of only HREEs in the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium).\| ii. Within the use of only LREEs for the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium), some LREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual LREEs are selected. For example, the subset may include three LREEs. The calculation (equation 2) is conducted for each of the 3 LREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 LREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [yttrium, scandium, lanthanum], [cerium, lanthanum, neodymium], [cerium, neodymium, samarium], [yttrium, cerium, neodymium], [scandium, neodymium, samarium].\| iii. Within the use of only HREEs for the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium), some HREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual HREEs are selected. For example, the subset may include three HREEs. The calculation (equation 2a) is conducted for each of the 3 HREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 HREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [europium, gadolinium, terbium], [europium, terbium, dysprosium], [dysprosium, erbium, ytterbium], [europium, erbium, ytterbium], [europium, dysprosium, erbium].\| iv. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual REEs are selected. For example, the subset may include three REEs Chart 1 represents a non-limiting list of REE triplicates that may enhance the efficacy of this C drawdown calculation.Chart 1. A non-limiting list of 455 REE triplicates that can be used to effectively triangulate a C drawdown estimation\|('Y', 'La', 'Ce'), ('Y', 'La', 'Pr'), ('Y', 'La', 'Nd'), ('Y', 'La', 'Sm'), ('Y', 'La', 'Eu'), ('Y', 'La', 'Gd'), ('Y', 'La', 'Tb'), ('Y', 'La', 'Dy'), ('Y', 'La', 'Ho'), ('Y', 'La', 'Er'), ('Y', 'La', 'Tm'), ('Y', 'La', 'Yb'), ('Y', 'La', 'Lu'), ('Y', 'Ce', 'Pr'), ('Y', 'Ce', 'Nd'), ('Y', 'Ce', 'Sm'), ('Y', 'Ce', 'Eu'), ('Y', 'Ce', 'Gd'), ('Y', 'Ce', 'Tb' ), ('Y', 'Ce', 'Dy'), ('Y', 'Ce', 'Ho'), ('Y', 'Ce', 'Er'), ('Y', 'Ce', 'Tm'), ('Y', 'Ce', 'Yb'), ('Y', 'Ce', 'Lu'), (' Y', 'Pr', 'Nd'), ('Y', 'Pr', 'Sm'), ('Y', 'Pr', 'Eu'), ('Y', 'Pr', 'Gd'), ('Y', 'Pr', 'Tb'), ('Y', 'Pr', 'Dy'), ('Y', 'Pr ', 'Ho'), ('Y', 'Pr', 'Er'), ('Y', 'Pr', 'Tm'), ('Y', 'Pr', 'Yb'), ('Y', 'Pr', 'Lu'), ('Y', 'Nd', 'Sm'), ('Y', 'Nd', 'E u'), ('Y', 'Nd', 'Gd'), ('Y', 'Nd', 'Tb'), ('Y', 'Nd', 'Dy'), ('Y', 'Nd', 'Ho'), ('Y', 'Nd', 'Er'), ('Y', 'Nd', 'Tm' ), ('Y', 'Nd', 'Yb'), ('Y', 'Nd', 'Lu'), ('Y', 'Sm', 'Eu'), ('Y', 'Sm', 'Gd'), ('Y', 'Sm', 'Tb'), ('Y', 'Sm', 'Dy'), ('Y', 'Sm', 'Ho'), ('Y', 'Sm', 'Er'), ('Y', 'Sm', 'Tm'), ('Y', 'Sm', 'Yb'), ('Y', 'Sm', 'Lu'), ('Y', 'Eu', 'Gd'), ('Y', 'Eu', 'Tb'), ('Y', 'Eu', 'Dy'), ('Y', 'Eu', 'Ho'), ('Y', 'Eu', 'Er'), ('Y', 'Eu', 'Tm'), ('Y', 'Eu', 'Yb'), ('Y ', 'Eu', 'Lu'), ('Y', 'Gd', 'Tb'), ('Y', 'Gd', 'Dy'), ('Y', 'Gd', 'Ho'), ('Y', 'Gd', 'Er'), ('Y', 'Gd', 'Tm'), ('Y', ' Gd', 'Yb'), ('Y', 'Gd', 'Lu'), ('Y', 'Tb', 'Dy'), ('Y', 'Tb', 'Ho'), ('Y', 'Tb', 'Er'), ('Y', 'Tb', 'Tm'), ('Y', 'Tb ', 'Yb'), ('Y', 'Tb', 'Lu'), ('Y', 'Dy', 'Ho'), ('Y', 'Dy', 'Er'), ('Y', 'Dy', 'Tm'), ('Y', 'Dy', 'Yb'), ('Y', 'Dy', 'Lu'), ('Y', 'Ho', 'Er'), ('Y', 'Ho', 'Tm'), ('Y', 'Ho', 'Yb'), ('Y', 'Ho', 'Lu'), ('Y', 'Er', 'Tm'), ('Y', 'Er', 'Y b'), ('Y', 'Er', 'Lu'), ('Y', 'Tm', 'Yb'), ('Y', 'Tm', 'Lu'), ('Y', 'Yb', 'Lu'), ('La', 'Ce', 'Pr'), ('La', 'Ce', 'Nd' ), ('La', 'Ce', 'Sm'), ('La', 'Ce', 'Eu'), ('La', 'Ce', 'Gd'), ('La', 'Ce', 'Tb'), ('La', 'Ce', 'Dy'), ('La', 'Ce', ' Ho'), ('La', 'Ce', 'Er'), ('La', 'Ce', 'Tm'), ('La', 'Ce', 'Yb'), ('La', 'Ce', 'Lu'), ('La', 'Pr', 'Nd'), ('La', 'Pr', 'Sm'), ('La', 'Pr', 'Eu'), ('La', 'Pr', 'Gd'), ('La', 'Pr', 'Tb'), ('La', 'Pr', 'Dy'), ('La', 'Pr', 'Ho'), ('La', 'Pr', ' Er'), ('La', 'Pr', 'Tm'), ('La', 'Pr', 'Yb'), ('La', 'Pr', 'Lu'), ('La', 'Nd', 'Sm'), ('La', 'Nd', 'Eu'), ('La', 'Nd', 'Gd'), ('La', 'Nd', 'Tb'), ('La', 'Nd', 'Dy'), ('La', 'Nd', 'Ho'), ('La', 'Nd', 'Er'), ('La', 'Nd', 'Tm'), ('La', ' Nd', 'Yb'), ('La', 'Nd', 'Lu'), ('La', 'Sm', 'Eu'), ('La', 'Sm', 'Gd'), ('La', 'Sm', 'Tb'), ('La', 'Sm', 'Dy'), (' La', 'Sm', 'Ho'), ('La', 'Sm', 'Er'), ('La', 'Sm', 'Tm'), ('La', 'Sm', 'Yb'), ('La', 'Sm', 'Lu'), ('La', 'Eu', 'G d'), ('La', 'Eu', 'Tb'), ('La', 'Eu', 'Dy'), ('La', 'Eu', 'Ho'), ('La', 'Eu', 'Er'), ('La', 'Eu', 'Tm'), ('La', 'Eu', ' Yb'), ('La', 'Eu', 'Lu'), ('La', 'Gd', 'Tb'), ('La', 'Gd', 'Dy'), ('La', 'Gd', 'Ho'), ('La', 'Gd', 'Er'), ('La', 'G d', 'Tm'), ('La', 'Gd', 'Yb'), ('La', 'Gd', 'Lu'), 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'Gd', 'Er'), ('Sm', 'Gd', 'Tm'), ('Sm ', 'Gd', 'Yb'), ('Sm', 'Gd', 'Lu'), ('Sm', 'Tb', 'Dy'), ('Sm', 'Tb', 'Ho'), ('Sm', 'Tb', 'Er'), ('Sm', 'Tb', 'Tm' ), ('Sm', 'Tb', 'Yb'), ('Sm', 'Tb', 'Lu'), ('Sm', 'Dy', 'Ho'), ('Sm', 'Dy', 'Er'), ('Sm', 'Dy', 'Tm'), ('Sm', 'D y', 'Yb'), ('Sm', 'Dy', 'Lu'), ('Sm', 'Ho', 'Er'), ('Sm', 'Ho', 'Tm'), ('Sm', 'Ho', 'Yb'), ('Sm', 'Ho', 'Lu'), (' Sm', 'Er', 'Tm'), ('Sm', 'Er', 'Yb'), ('Sm', 'Er', 'Lu'), ('Sm', 'Tm', 'Yb'), ('Sm', 'Tm', 'Lu'), ('Sm', 'Yb', ' Lu'), ('Eu', 'Gd', 'Tb'), ('Eu', 'Gd', 'Dy'), ('Eu', 'Gd', 'Ho'), ('Eu', 'Gd', 'Er'), ('Eu', 'Gd', 'Tm'), ('Eu', ' Gd', 'Yb'), ('Eu', 'Gd', 'Lu'), ('Eu', 'Tb', 'Dy'), ('Eu', 'Tb', 'Ho'), ('Eu', 'Tb', 'Er'), ('Eu', 'Tb', 'Tm'), ('E u', 'Tb', 'Yb'), ('Eu', 'Tb', 'Lu'), ('Eu', 'Dy', 'Ho'), ('Eu', 'Dy', 'Er'), ('Eu', 'Dy', 'Tm'), ('Eu', 'Dy', 'Yb'), ('Eu', 'Dy', 'Lu'), ('Eu', 'Ho', 'Er'), ('Eu', 'Ho', 'Tm'), ('Eu', 'Ho', 'Yb'), ('Eu', 'Ho', 'Lu'), ('Eu', 'Er', 'T m'), ('Eu', 'Er', 'Yb'), ('Eu', 'Er', 'Lu'), ('Eu', 'Tm', 'Yb'), ('Eu', 'Tm', 'Lu'), ('Eu', 'Yb', 'Lu'), ('Gd', 'Tb ', 'Dy'), ('Gd', 'Tb', 'Ho'), ('Gd', 'Tb', 'Er'), ('Gd', 'Tb', 'Tm'), ('Gd', 'Tb', 'Yb'), ('Gd', 'Tb', 'Lu'), ('Gd', 'Dy', 'Ho'), ('Gd', 'Dy', 'Er'), ('Gd', 'Dy', 'Tm'), ('Gd', 'Dy', 'Yb'), ('Gd', 'Dy', 'Lu'), ('Gd', 'Ho', 'Er'), ('Gd', 'Ho', 'Tm'), ('Gd', 'Ho', 'Yb'), ('Gd', 'Ho', 'Lu'), ('Gd', 'Er', 'Tm'), ('Gd', 'Er', 'Yb'), ('Gd', 'Er', ' Lu'), ('Gd', 'Tm', 'Yb'), ('Gd', 'Tm', 'Lu'), ('Gd', 'Yb', 'Lu'), ('Tb', 'Dy', 'Ho'), ('Tb', 'Dy', 'Er'), ('Tb', ' Dy', 'Tm'), ('Tb', 'Dy', 'Yb'), ('Tb', 'Dy', 'Lu'), ('Tb', 'Ho', 'Er'), ('Tb', 'Ho', 'Tm'), ('Tb', 'Ho', 'Yb'), (' Tb', 'Ho', 'Lu'), ('Tb', 'Er', 'Tm'), ('Tb', 'Er', 'Yb'), ('Tb', 'Er', 'Lu'), ('Tb', 'Tm', 'Yb'), ('Tb', 'Tm', 'Lu' ), ('Tb', 'Yb', 'Lu'), ('Dy', 'Ho', 'Er'), ('Dy', 'Ho', 'Tm'), ('Dy', 'Ho', 'Yb'), ('Dy', 'Ho', 'Lu'), ('Dy', 'Er', 'Tm'), ('Dy', 'Er', 'Yb'), ('Dy', 'Er', 'Lu'), ('Dy', 'Tm', 'Yb'), ('Dy', 'Tm', 'Lu'), ('Dy', 'Yb', 'Lu'), ('Ho', 'Er', 'Tm'), ('Ho', 'Er', 'Yb'), ('Ho', 'Er', 'Lu'), ('Ho', 'Tm', 'Yb'), ('Ho', 'Tm', 'Lu'), ('Ho', 'Yb', 'Lu'), (' Er', 'Tm', 'Yb'), ('Er', 'Tm', 'Lu'), ('Er', 'Yb', 'Lu'), ('Tm', 'Yb', 'Lu') 3. Example Verification methodology 3: this methodology expands on Verification methodology 2 by the use of naturally occurring microbial cation exchangers, including bacteria and fungi.i. As above but right before step vii (unsealing samples in laboratory), add the following steps:\| ii. Lyse the microbes. For example, autoclave each sample-containing beaker for steam sterilization at 250 °F at 15 psi for 15 minutes. This may lyse any microbes and cause an active release of bio-adsorbed metals.\| iii. Let sample-containing beakers cool to room temperature before proceeding.\| iv. The filter in step (ix) may now act to additionally remove any larger aggregates of microbial cell suspensions that did not lyse in the autoclaving process.\| v. The added EDTA in step (x) in Verification Methodology 2 may act to additionally chelate any REEs that are complexed to the cell wall or organic molecules of the microbial genetic material (as a result of cell lysis).\| vi. In conjunction, verification methodology 3 provides a protocol to achieve full recovery of REEs that were retained in the top 10 cm of soil due to the following biogeochemical processes:1. Mineral surface interface complexation.\| 2. The cation exchange capacity inherent to soils due to organic matter.\| 3. Microbially mediated surface biosorption and/or active biological absorption pathways including but not limited to REE-aqueous complexation with internal genetic material of individual microbial cells found in natural soils and sediments. B. Example systems and methods to enhance the agronomic performance and ecosystem co-benefits:In these non-limiting embodiments, product formulations are detailed that improve the soil quality for improved agronomic applications as well as embodiments that specify improvements on crop health and an ability for plants to protect themselves from pathogens.\| Addition of macronutrients that enhance the agronomic benefits of the applied mineral. Example: addition of elemental 1-5% by weight formulation K or Ca or inexpensive REE such as La to improve use cases of pulverized Mg2SiO4 by improving the nutrient balance of the soil to match the needs of actively growing plants. Application rates for K and Ca may range from 50-100 ppm and lanthanide addition rates may range from 1-50 ppm.\| The 1-5% by volume addition of slow-release acidifiers in the form of elements that maintain the acidity of the soil despite the tendency of the applied mineral to reduce soil acidity in the weathering process. Example: addition of minerals with Al (such as gibbsite, Al(OH)3) or S (such as gypsum, CaSO4)-2H2O), in a rate of 1-10% by weight of total formulation, which contribute to maintaining soil acidity, and thus maintain high rates of weathering, which counteracts the tendency of forsterite weathering to increase alkalinity, which slows rates of weathering.\| The incorporation of additional micronutrients such as zinc (1-5% by weight compared to mineral amendment) to reduce ecosystem losses of phosphorus and downstream ecosystem impacts of phosphate-based fertilizers, such as eutrophication. Phosphates are immobilized via precipitation reactions with the additional zinc metal, so zinc addition slows the transport and reduces mobility of phosphate in the subsoil. As a consequence, phosphate-based fertilizer applications can be performed more safely and with higher confidence that downstream waterways will not form algal blooms and lead to anoxic, uninhabitable waterways for aquatic life. The addition of 1-32 tons/hectare of mineral in conjunction with 1-5% by weight zinc in fields with heavy phosphate application reduces the likelihood of significant phosphate leaching. This also increases nutrient use efficiency, which reduces fertilizer cost to farmers and reduces negative environmental impacts to society. Specifically, phosphate-zinc precipitates become slow-releasing over time due to their immobilization in the soil as a solid phase. This provides longer timeframes for plants to access the phosphate application, reducing the frequency of fertilization.\| The method of mixing of different mineral adjuvants to the primary mineral used for carbon removal can be varied, with impacts on performance. In some embodiments, the admixture (e.g., of gypsum and forsterite) could be completely emulsified. In some embodiments, a nutrient, such as urea, could represent a core that is subsequently coated with a shell of silicate mineral used for carbon removal. In some embodiments the silicate mineral could be the core, and the nutrient, such as urea, could be the coating. In each of these cases, the embodiment can be optimized so as to reduce environmental losses of the nutrient, and increase availability to the plant, while providing the acidity necessary for the silicate mineral weathering. In some embodiments, this may represent a "slow release" nutrient that does not mineralize too quickly and is synchronized more favorably with plant demand.\| Comminution, or pulverization, may help reproduce the expected kinetics of alkalizers such as pulverized limestone or dolomite, known as aglime. Aglime has well-characterized kinetics originating in the particle size distribution of the product, which are in some jurisdictions legally regulated to meet certain requirements. A representative cross section of dissolution kinetics based on actual aglime mesh size observations is depicted in FIG. 2.\|It naturally follows that agronomic performance expectations for silicate minerals used for ERW should follow similar reaction kinetics, particularly in the first year after application, while also meeting the goals for CDR. Thus, an ideal particle size distribution may be tuned to meet this goal. The following shows the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um, such as 90um, which closely approximates the alkalinity release dynamics for aglime.\| The small particle sizes produced by pulverization as above are valuable for performance as an aglime substitute and CDR mechanism, but introduce their own set of potential challenges. One potential challenge is that small particle sizes may fall within regulated categories such as PM10 or PM2.5; another potential challenge is the product may not be easily transferred from one vessel to another (so-called "flowability") because it has a tendency to settle into a compact mass; the product may also not be applied uniformly by extant farm equipment; potentially low uniformity application impacts the agronomic performance as well as the sampling density needed for carbon removal verification. In one potential formulation, the product is pelletized after pulverization, using a common binder such as lignosulfate in a 3-5% ratio by weight of the total formulation. The amount of binder may be optimized to improve performance characteristics during transport and application, but minimize the water and energy needed to dissolve the pellet once it is in the field. Pelletizing the product, into a size range of, for example, 0.5 mm to 3 mm increases the flowability; reduces the prevalence of dust, including the risk of asbestos exposure; enables the use of extant crop input application equipment; and improves the evenness of field distribution, which has the agronomic and carbon verification benefits identified. Pelletizing in this size range also ensures that an adequate number of pellets fall onto any land area which may subsequently be sampled for analysis.\| A desiccated but living biological compound, such as a mycorrhizal inoculum, may be used to coat the agglomerated and dried pellets, so as to enhance the dissolution of the pellet itself after application. This may be distinct from a fungal adjuvant to the pellet to increase dissolution of the silicate minerals themselves.\| To accommodate a range of soil types from acidic to neutral pH, the product may be differentiated into different particle size distributions so as to achieve a consistent rate of weathering across different soil types. For example a consistent rate of weathering may be that the entire applied amount of mineral product weathers in 9 months, allowing a subsequent application every year. To achieve this, an acidic soil may have pellets that contain particles with a modal size on the order of 100 um, while a neutral soil may have pellets that contain particles with a modal size on the order of 10 um. The negative consequence of applying a fine particle in an acidic soil may be that it dissolves too quickly, swinging the pH of the soil too quickly, and altering the nutrient availability severely in the growing plant. The negative consequence of applying a coarse particle in a neutral soil may be that the particle weathers too slowly or is functionally inert, which does not remove carbon as intended, and may subject the farmer or the vendor to risk of clawbacks for payments received for carbon removal. C. Example systems and methods to control or enhance the performance as a securitized carbon removal method:In these non-limiting embodiments, product formulations are described that improve the marketability of pulverized and optionally pelletized mineral amendments as a verifiable carbon removal method, irrespective of their impact on agronomic performance. Such changes in marketability increase the value of the carbon product, for example for detecting and preventing fraud, or increase the dissolution rate (mass per area per year) to accelerate the timing of reapplication, which raises the value in a discounted cash flow analysis. The general scheme is depicted in FIG. 4.\| The addition of low cost and inert trace elements, for example 1-5 ppm neodymium or lanthanum, to a mineral amendment, beyond the natural abundances present in the ore body, improves performance in Verification methods 2 and 3. Specifically, the additional elements reduce measurement uncertainty owing to low natural abundance calculations as well as uncertainty owing to variability from the source mineral. Reduction of these uncertainties improves the detectability of true positives and true negatives. This principle could be applied to many potential soil amendments and fertilizers to verify provenance as pertains to legal contracts.\| The addition of binders to create aggregations of the ground mineral that could reduce drift, which improves distribution uniformity; reduces potential respiratory health impacts; and/or improves applicability of the applied mineral using commercially available equipment. For example, a biofilm mediating organic compound, such as alginate or chitosan, could be mixed with a pulverized mineral with a particle size of approximately 100 microns to achieve an aggregated pellet size of 1 millimeter. This would maintain the advantages of fine particle size, particularly the high specific surface area (m2/g) that mediates dissolution rate, while offsetting potential limitations outlined above. An example methodology for aggregating ground minerals could include these steps:∘ Dissolve 10 grams of alginate powder into solution to create a 0.5 M - 1.0 M alginic acid solution.\| ∘ Heat solution to 80-100 °F to dissolve alginate powder fully if necessary.\| ∘ Spray aerosol sized particles of dissolved alginate powder onto the ground rock material in order to create a biofilm-coated rock material. Apply a consistent spray of 100 mL for each 100 gram of rock (1:1 v/w).\| ∘ The resulting aggregates may have increased bulk density as well as higher aggregating properties due to van der Waals force attraction between the individual rock particles. Dissolution rates can be modified by non-living organic molecules applied concurrently with the mineral amendment. For example, protonated microbes such as acid-treated Arthrobacter nicotianae can constitute an initial release of protons to attack the ground rock materials' crystal structure. This method of acidification for optimal accelerated weathering of rock material may occur even during winter/cold climate. Because biologically mediated processes can have sharp thresholds, e.g., under freezing conditions, such a chemically controlled process would exhibit greater ability to expedite rock breakdown over a range of environmental conditions. To implement this methodology, we outline the following steps:1) De-frost an aliquot of A. nicotianae in 5 mL of Luria broth for about 24 hours at exactly 30 °C.\| 2) Sub-culture into a larger volume of Luria broth at a 1:50 dilution and allow growth for another 24 hours at 30 °C.\| 3) During growth steps #1 and 2, cultures may be shaken, for example at 200-220 RPM, for aeration.\| 4) After culture has been grown for 48 hours in total, centrifuge the cell suspension.\| 5) Collect cell pellet and take a small amount and set it aside. Weigh wet weight, dry at 60 °C overnight, and weigh dry amount to obtain wet : dry conversion.\| 6) Develop an OD600 to wet weight to dry weight conversion by taking 5 varying amounts of wet aliquots of wet biomass and measuring optical density given its known wet mass. Wet aliquots may have a mass of about 1, 4, 8, 12, 16 wet grams and be suspended in 100 mL of DI water.\| 7) Wash cells in 0.1 M NaCl solution.a. Centrifuge cells+growth media at 4000xg.\| b. Carefully pour out LB broth.\| c. Add 0.1 M NaCl solution.\| d. Centrifuge cells+NaCl solution at 4000xg.\| e. Carefully pour out NaCl solution. 8) Protonate the cells while wet.a. Re-suspend the wet biomass in an acidic (e.g., pH 3.0) solution using a dilute hydrochloric acid solution (0.001-0.01 M).\| b. Centrifuge cells+HCl solution at 4000xg.\| c. Carefully pour out solution.\| d. Repeat steps (a)-(c) a total of three times.\| e. Dry cells in an oven at 80-100 °C for 48 hours.\| f. Grind cells using a mortar/pestle to achieve a powder form. 9) Mix 5% w/w of dry cell powder with the ground rock material.\| 10) When this particular rock material+cell powder mixture is applied to agricultural soils, the irrigation or rainfall will re-apply moisture and allow the pre-protonated, re-wet biomass to release their protons. This will ultimately induce a local acidity effect on the rock particle (molecular) level to accelerate rock crystal lattice breakdown. The cells act as biodegradable transporters that are also benign to the natural soil environment.	(EP4256520)\|Cross Reference to Related Applications\|[0001] The present applications claims the priority benefit of U.S. Provisional Patent App. Serial No. 63/322,672, filed March 23, 2022; U.S. Provisional Patent App. Serial No. 63/289,395, filed December 14, 2021; and U.S. Provisional Patent App. Serial No. 63/213,398, filed, June 22, 2021.\|Background\|[0002] The last several years have witnessed a maturation of carbon markets from lightly scrutinized voluntary markets largely serving to provide positive marketing collateral to familiar consumer brands to rigorous compliance markets with proof-of-performance requirements often involving government and quasi-governmental regulators. There have also been a number of comprehensive proposals for decarbonization of the entire US economy, combining energy production, transportation, cement production, and agriculture. These proposals have included carbon dioxide removal (CDR) techniques as an essential component of the decarbonization plan, with a supportive ecosystem of science, policy, and project evaluation criteria. Within the diverse scope of decarbonization efforts, including renewable energy, biofuel, nature-based solutions, and more technical CDR techniques like direct air capture (DAC), The Oxford Principles have developed a taxonomy for categorizing diverse decarbonization strategies. This taxonomy distinguishes between avoided emissions (for instance, conversion of fossil fuel power to renewable power) and negative emissions (for instance direct air capture); distinguishes between avoided emissions that require storage (for instance carbon capture from a point source and sequestration into the ground) and those that do not require storage (the conversion to renewable energy); and the duration of the storage if so required (for instance, short lived forest carbon sequestration from delayed harvests versus storage of captured carbon in geological formations).\|[0003] A number of for-profit and non-profit organizations have emerged that employ the Oxford Principles to evaluate proposals, particularly around the rigorous quantification across categories (Table 1). This, in essence, is the scorecard that projects will have to compete on to find acceptance in the industry. All other things equal, cost ends up being the primary driver, but quality is also a key consideration. Thus, historically buyers have been drawn to nature-based solutions that cost between $5-20/tCO2 e (e.g., Corteva Carbon, Indigo Carbon), versus direct air capture projects that cost >$500/tCO2 e (e.g., ClimeWorks). However, there are challenges to these nature-based solutions: recently these nature-based solutions have been subject to intense scrutiny for "gaming" the rules or otherwise failing to deliver prospective rewards. Among the technological solutions, there are a different set of challenges: rigor has been strong, but the reduction in price proportional to increase in deployment has been slow, and the ultimate price of DAC is not expected to drop below $150/tCO2e (Keith et al 2018, https://doi.org/10.1016/j.joule.2018.05.006). In light of these challenges, we have developed a technology around "enhanced rock weathering" (ERW), in which silicate minerals are weathered in acidic soil solution, thus driving the uptake of additional CO2 into dissolved inorganic carbon (DIC) in the soil solution. Our experimental work, life cycle analysis, and techno-economic modeling have indicated that ERW provides the permanence, additionality, and rigorous quantification of a DAC project, the large volume of a carbon capture and storage (CCS) project, and the unit economics of a nature based solution, thus creating a new tool to meet net-zero goals.\|Details of Enhanced Rock Weathering\|[0004] In "enhanced rock weathering" (ERW), silicate minerals are weathered by CO2 from the ambient air which has been dissolved into water, reacting to produce dissolved inorganic carbon that is ultimately stored in the ocean as depicted in FIGS. 1 and 2.\|Background Geochemistry\|[0005] The role of silicate rock weathering in maintaining the CO2 balance of the atmosphere has been recognized for decades, first outlined by renowned chemist Harold Urey in the 1950s. The basic premise of the Urey reaction is that continental collisions release CO2 to the atmosphere from volcanoes, and bring Mg- and Ca-bearing silicate rocks to the surface. The rainwater (H2O) that falls upon these rocks is mildly acidic, as atmospheric CO2 has dissolved in it and formed carbonic acid (H2CO3). For forsterite, the weathering reaction takes place following the form:\| Mg2SiO4 + 4 H2O + 4 CO2 → 2 Mg2+ + 4 HCO3- + 4 H4SiO4\|[0006] In this reaction, one mole of forsterite consumes four moles of CO2, so two negatively charged bicarbonate HCO3- are created for every one divalent Mg2+ weathered. Given the molecular weight of forsterite (140 g/mol) and the molecular weight of CO2 (44 g/mol), weathering one metric ton of forsterite removes 1.25 metric tons of CO2 from the atmosphere. In general, such a formula can be used to define the "mineral potential" of a silicate based on its elemental composition: \| where V is the valence of the cation (2 for Mg and Ca) and MW is the molecular weight.\|[0007] The rate of weathering is determined by the surface area of the mineral, the acidity (pH) of the soil solution, the temperature of the solution, the availability of CO2 reagent in solution, and the rate of removal of the reaction products by water. One of the key insights into the potential of "enhanced" rock weathering is that the rate of reaction, and thus CO2 removal, can be greatly accelerated by increasing the surface area by pulverization into a fine powder (e.g., less than 100 um), incorporating into an acidic environment (e.g., pH less than 6) with abundant CO2 present, and with steady water flux to remove reaction products to maintain acidity. While this formula defines the potential amount of CO2 that may be removed by weathering, it does not speak to the rate; ancient rock formations testify that the rate of weathering can be extremely slow.\|[0008] The relationship between silicates (like Mg2SiO4) and dissolved carbonates (like HCO3-) is not necessarily intuitive, as the carbonate system of water involves a number of coupled reactions. Atmospheric CO2 dissolves into water according to an exchange coefficient:\| CO2(aq) = H2CO3 = KCO2 * pCO2\|[0009] Technically pCO2 is "fugacity" that represents its activity, but, as used herein, it is more or less equivalent to its partial pressure, and KCO2 is the Henry's law coefficient that determines the aqueous CO2 in equilibrium with the atmosphere. This aqueous CO2 in turn hydrates with H2O to become carbonic acid (H2CO3), which dissociates to become bicarbonate (HCO3-) and carbonate (CO32-):\| H2CO3 ↔ HCO3- + H+\| HCO3- ↔ CO32- + H+\|[0010] These equilibrium reactions are defined by K1 and K2, the first and second carbonate system dissociation constants. pK1 and pK2 are about 5.9 and about 9.4 at STP, so greater than 99% of the charge in the dissolved carbonates is HCO3-.\|[0011] The carbonates are the largest constituents of total alkalinity, which is defined as the charge imbalance between weak acids (proton acceptors) minus proton donors:\| TA = [HCO3-] + 2 · [CO32-] + [OH-] - [H+]\|[0012] There is an alternative definition of total alkalinity as the charge imbalance between conserved cations and conserved anions:\| TA = [Na+] + 2 [Mg2+] + 2 [Ca2+] + [K+] + ... - [Cl-] - 2 [SO42-] - [NO3-]\|[0013] These two expressions are always equal (i.e. the charges balance). This means that an added Mg or Ca into soil solution will increase in HCO3- to balance the charge. We describe an analytical solution to compute how much carbon is taken up per unit of additional Mg or Ca. If we first define DIC as the sum of H2CO3, HCO3-, and CO32-, and make use of the equilibrium equations above (defining H+ as "h" and H2CO3 as "s"): \|[0014] And formulate TA using the same convention: \|[0015] With these definitions in place, we can develop an estimate of dDIC/dTA. First, we compute the derivative dTA/dh: \|[0016] Next we compute the derivative dDIC/dh: \|[0017] Finally we multiply dDIC/dh by the inverse of dTA/dh to calculate dDIC/dTA: \|[0018] At the pH found in soils, each Mg or Ca is matched by two carbon atoms. In all circumstances, raising alkalinity results in increased pH. This is particularly important in marine settings, where ocean acidification from increased atmospheric CO2 can be ameliorated by this export of alkalinity from land.\|[0019] The potential for ERW as a commercial enterprise is limited by some fundamental issues:\| A. The total amounts of mineral transformation and carbon removal should be verifiable empirically. The verification methods described below may be low cost at scale, can be performed at arm's length by a 3rd party, and may have safeguards to eliminate fraud.\|[0020] Additionally, the commercial potential for ERW could be enhanced by a number of different features. Embodiments may include:\| B. Processes and modifications of the engineered mineral product that enhance the agronomic performance and ecosystem co-benefits of the engineered mineral.\| C. Processes and modifications of the engineered mineral product that control or enhance the mineral dissolution rate of the engineered mineral in soil environments and thus the rate of removal of CO2.\| C. Paulo et al, Applied Geochemistry, 2021, 219, 104955, discusses evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralisation.\| N. Moosdorf et al, Environ. Sci. Tech., 2014, 48, 4809 discusses carbon dioxide efficiency of terrestrial enhanced weathering and determination of effective carbon dioxide sequestration.\|Brief Description of the Drawings\|[0021] FIG. 1 is a drawing illustrating the enhanced rock weathering cycle.\| FIG. 2 is a graph depicting the effect of comminution on dissolution kinetics for a silicate.\| FIGS. 3A to 3D are graphs depicting the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um which closely approximates the alkalinity release dynamics for aglime.\| FIG. 4 is a drawing illustrating the general scheme for a verified enhanced rock weathering cycle.\|Detailed Description\|[0022] Summary: The following described methodologies can establish one version of a verification scheme that will demonstrate the transformation of the applied rock material and the subsequent carbon removal into secure geologic reservoirs as evidenced by observations collected from the soil. One set of methods (A) can measure the production of free ions from the applied material and the transport of those ions outside of a control volume as a direct measure of the amount of weathering and thus total carbon dioxide equivalent isolated from the atmosphere. Furthermore, as the elemental inputs into the soil induced by enhanced rock weathering can have significant effects on the soil geochemistry, methods in (B) describe systems and versions that can enhance the agronomic performance of the soil amendment and increase ecosystem co-benefits. Lastly, methods in (C) elaborate on versions that control and enhance the mineral dissolution rate, which increases the financial performance of enhanced rock weathering technology in the marketplace.\| A. Systems and methods for monitoring and verification:Described below are several example methodologies for quantifying the rate and extent of mineral transformation and carbon removal, which are referred to as "verification methodologies".1. Example Verification methodology 1:a. A cation exchange resin and/or an anion exchange resin are packaged into a physical embodiment (such as a 5 cm diameter tube, 5cm in length, placed 30 cm below the soil surface) that allows vertical transport of fluids but not horizontal transport.\| b. Commercial ion exchange resins are pre-equilibrated in such a way that their selectivity is high for the relevant ions, but their capacity is also sufficiently high such that saturation is minimized. This technology may allow for effective deployment for long periods of time, allowing passage of up to 4000 mm of moisture through the tube, without becoming saturated with respect to the ions of interest.\| c. The ions of interest are restricted to divalent cations (Mg2+, Ca2+), carbonate species (HCO3- and CO32-), and silicic acid (H4SiO4), important weathering products of preferred mineral soil amendments, such as ultramafic rocks, blast furnace slag, and other naturally occurring or industrial silicate minerals with high Mg and Ca content.\| d. Three pre-equilibrated tubes are emplaced fully under the soil below a control depth (e.g., 30 cm, a typical depth of cultivation). This may be done by removing the top 30 cm soil with a shovel or auger, then gently placing the tube in the created void space. Following a certain period of time post-surface application of mineral soil amendment (e.g., 9 to 12 months after application), the tubes are retrieved, and the ions captured within the resin exchanges are measured using standard methodologies, such as ICP-OES and ICP-MS based concentration measurements. Three tubes are used to determine standard deviation error in triplicate.\| e. By the principle of charge balance and known thermodynamic reactions taking place in the top 30 cm of soils, the amount of carbonate can be inferred purely from the measurement of cations, under certain assumptions and auxiliary geochemical data. By the addition of more specific anion exchange resins, such as styrenedivinylbenzene, these assumptions can be avoided to get a more precise answer. The increase in cation concentration in the subsurface soil pore water allows for the stoichiometric determination of carbon removal from the gas phase (ambient air).\| f. The total carbon dioxide removed during the deployment period may be estimated as equal to the molecular mass of CO2 (44 g/mol) multiplied by the sum of the number of moles of carbonate and two times the number of moles of bicarbonate, multiplied by the area on which mineral was applied to the field, divided by the cross-sectional area of the tube.\| g. Direct measurement of aqueous bicarbonate and carbonate species, which are the most readily available forms of carbon induced by a gas exchange of carbon dioxide with the soil pore water, may be conducted using the specified anion exchange resin above. The expression as described in clause (f) explains the calculation used to convert this direct measurement of carbon to an absolute value of carbon dioxide removed during a specified application period.\| h. Verification methodology 1 has the advantage that it can provide a direct measure of carbon flux and employs a measurement technique that is mature.\| i. However, potential disadvantages may include the need for manufacturing (and its attendant demand for working capital); devices may occasionally be defective; emplacement of a device may alter the flow paths of water, which in turn alters the inferred ion fluxes; emplacement of a device may depend on the user; the knowledge of the location of emplacement may invite manipulation by a stakeholder involved in a carbon transaction; and others. 2. Example Verification methodology 2:a. The principle behind Verification methodology 2 is that minerals applied for purposes of enhanced rock weathering contain, in addition to the elements outlined above that participate in the weathering reaction (i.e., magnesium, calcium, iron, silicon, oxygen, hydrogen), additional elements in trace amounts. These additional trace elements (TEs) might include rare earth elements (REEs), rare metals (RM), other transition metals (TMs), or a combination thereof. Unlike the primary weathering products that are readily dissolved in solution and lost by leaching, some TEs are strongly bound to mineral and biological surfaces and do not readily leach from the soil control volume (e.g., the top 10 to 30 cm of soil), and are not removed by plants at the concentrations present in our applied rock. These strongly bound trace elements are referred to herein as immobile trace elements (ITEs). Thus, a measure of cumulative cation flux and carbon removal can be computed by comparing the ratio of the lost weathering products, such as magnesium, to ITEs, after accounting for background concentrations of ITEs in the initial soil.\| b. As used herein, rare earth elements include scandium (Sc), yttrium (Y), lanthanum (La), cerium (Ce), praseodymium (Pr), neodymium (Nd), samarium (Sm), europium (Eu), gadolinium (Gd), terbium (Tb), dysprosium (Dy), holmium (Ho), erbium (Er), thulium (Tm), ytterbium (Yb), lutetium (Lu) or a combination thereof. As used herein, rare metals include beryllium (Be), cesium (Cs), gallium (Ga), germanium (Ge), hafnium (Hf), niobium (Nb), rubidium (Rb), tantalum (Ta), zirconium (Zr), or a combination thereof. As used herein, transition metals include nickel (Ni), chromium (Cr), and zinc (Zn) among others and may include a combination of transition metals.\| c. An approach based on ITEs depends on the degree of immobility of the element in soil environments, the time horizon after which the ITEs will be measured to estimate carbon removal, the abundance of ITEs in both the soil and the mineral added, and the analytical chemistry used to measure this abundance. An analytical technique that has low detectability thresholds for slightly mobile elements could be sufficient for relatively abundant (e.g., parts per thousand to parts per million) elements over short time horizons (e.g., weeks to months). On the other hand, a different analytical technique could be used over longer time horizons, which in turn could involve quantification of very immobile elements that are present in much lower abundance (e.g., parts per billion to parts per trillion). The approach may be chosen based at least in part on cost, which ITEs are actually conserved, over which time horizons, as well as the performance of the analytical performance used.\| d. The relative proportions of ITEs in a sample (rock or soil) constitute a type of unique fingerprint of the material. Because the cost of pure ITEs is large, and the analytical chemistry is not widely available, there is a significant barrier to engineering a fraudulent sample to reproduce the native ITE fingerprint of a mineral soil amendment. Thus, it would be challenging for a stakeholder in a carbon exchange transaction to generate a result that produces the anticipated result (a high or low amount of carbon removal) while also matching the ITE fingerprint generated by a bona fide sample. This is a contrast with measurement schemes for soil organic carbon, in which the landowner or other interested party has an information advantage in terms of where or when to sample, which could be used to achieve a particular carbon measurement objective (high or low).\| e. Verification Methodology 2 (VM2) has advantages over Verification Methodology 1 (VM1) in that it avoids the need for the use of a device, which avoids altering the soil hydrology or physical environment in a way that would impact the observed elemental analysis.\| f. VM2 may have an advantage over VM1 in not requiring tracking of a specific location for recovering the sampling column.\| g. VM2 does, however, include measurement techniques that are less widely available; requires specialized instruments and personnel; requires additional boundary conditions to compute carbon flux (e.g., pre-application soil and rock elemental analysis); and employs assumptions as to the relationship between cation flux and carbon flux.\| h. Like VM1, VM2 uses the total amount of mineral applied and the field area, which could be measured, for example, using a digital as-applied map commonly accompanying crops input machinery, or truck weights before and after mineral delivery. This will be referred to as the nominal application rate (ARnominal).\| i. There are four main calculations in VM2. To the extent any one of these factors is known unambiguously from other sources, each step in VM2 could be used in isolation from the others.i. Classify, using ITE fingerprinting, whether a soil has had a specific mineral applied, which may be asserted by an entity wishing to make a claim;\| ii. Calculate, using ITE fingerprinting, what the actual mineral application rate (ARactual) for a specific soil sample was, which will necessarily differ in a systematic or random way from the average rate for the entire field;\| iii. Calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the application rate in (ii) above;\| iv. Calculate, using the fraction computed in (iii) and the mineral potential (Equation 1) computed for the feedstock identified in (i) above, the amount of carbon dioxide removed. j. In one non-limiting embodiment, the verification methodology to classify whether the claimed mineral applied is the actual mineral applied is as follows:i. Collect a sample from mineral to be applied, place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Mineral Amendment.\| ii. Prior to mineral application, collect a 20 g sample from cultivated zone of soil (typically at around 30 cm, such as in a range of 0 cm to 30 cm), place in a secure vessel and seal with another secondary bag in order to reach air-tight containment. Label as Soil A.\| iii. Subsequent to mineral application, collect a 20 g sample the same control zone as soil A, and store under similar conditions. Label as Soil B. Soil B could be sampled immediately after mineral application or at a later time (e.g., months to years afterwards).\| iv. Characterize the elemental composition of Mineral Amendment, Soil A, and Soil B. Example approaches to characterizing the elemental composition are described in (v) and (vi).\| v. One approach to measuring the elemental composition is as follows:1. In a laboratory setting, unseal the soil samples and place 10 grams of Soil A and Soil B in two separate beakers.\| 2. Dissolve the solids in strong acid. For example, add 21 mL of strong 1.0 M hydrochloric acid and 7 mL of strong 1.0 M nitric acid (total 28 mL acid) to each beaker of sterilized soil and stir rigorously until solids are dissolved.\| 3. Filter the sample-containing beakers first through a 1- to 5-micron water filter cartridge followed by an attached 10 to 20 cm column cation exchange resin at a sufficiently slow flow rate of, for example, 1 to 5 mL/min. This combination of a water filter with a cation exchange column has been engineered for optimal performance with soils under consideration. Specifically, the 5-micron water filter cartridge separates out any larger particles, allowing for the smaller particles to exchange its bound metals with the subsequent cation exchange resin.\| 4. Flush copious amounts (e.g., 100-200 mL) of 0.5 to 1.0 M chelator such as, for example, ethylenediaminetetraacetic acid (EDTA) at 1-5 mL/min through the used filters into their respective filtrates. This may collect any additional metals that were still adhered to the filters.\| 5. Send filtrate A (resultant sample from Soil A) and filtrate B (resultant sample from Soil B) to an analytical laboratory for analysis on an inductively coupled plasma mass spectrometer (ICP-MS). Measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3.\| 6. The ICP-MS may be set to detect magnesium concentrations and the following 17 elements on a high ppb or low ppm detection level: Yttrium, Scandium, Lanthanum, Cerium, Praseodymium, Neodymium, Promethium, Samarium, Europium, Gadolinium, Terbium, Dysprosium, Holmium, Erbium, Thulium, Ytterbium, Lutetium. Classify light rare earth elements (LREEs) as yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium. Classify heavy rare earth elements (HREEs) as europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium. Send an isolated rock material sample for ICP-MS analysis. Similar to the filtrate analyses, measurements may include concentrations of high ppb detection of REEs, high ppm detection of Mg, and percent mineralogical fractions of SiO2, Al2O3, and Fe2O3. vi. Another approach to measuring the elemental composition is as follows:1. Calibrate a portable XRF instrument for particularly low detection limit of ITEs using a calibration standard (such as Bruker proprietary Geo calibration + custom ITE standards).\| 2. Use the portable XRF instrument to analyze the Rock Material and Soil A for ITEs (as identified in Verification methodology 2), reporting the instrumental error (2 standard deviations) as well.\| 3. Use the portable XRF instrument to analyze Soil B for ITEs, reporting the instrumental error (2 standard deviations) as well. vii. Once the above elemental composition has been determined, calculate the difference for every element between Mineral Amendment and Soil A, resulting in a vector of differences vrock. Likewise, compute the difference for every element between Soil B and Soil A, resulting in a vector of differences vsoil. To improve performance, each element may be divided by an individual factor, such as the detection threshold, or the instrumental uncertainty, or the elemental composition of a reference material. Another means to improve performance would be to sum a subset of the elements or several distinct subsets of elements before computing vrock and vsoil. Another means to improve performance would be to compute indices of these summed subsets of elements, for example the ratio of the light REEs to the heavy REEs, before computing vrock and vsoil.\| viii. Compute the dot product of vrock and vsoil. If the value of this dot product is close to 1 (e.g., within a threshold value), then the Soil B is positively classified as having the Mineral Amendment. If the value of the dot product is less than 1 minus a threshold value, then Soil B is negatively classified as not having the Mineral Amendment.\| ix. The threshold value may be determined using a variety of means, for example the half-angle between the dot product of vrock and vsoil and any other known vrock and vsoil; or using a Monte Carlo simulation of vrock and vsoil that accounts for known sources of uncertainty including instrumental error, variation in rock elemental analysis, or variation of soil elemental analysis. k. In one non-limiting embodiment, the verification methodology to calculate the actual mineral application rate (ARactual) for a specific soil sample is as follows:i. Characterize the elemental composition the elemental composition of Mineral Amendment, Soil A, and Soil B as above. Note that there could be different analytical chemistry employed if, for example, rapid and inexpensive XRF analysis was used for classification soon after application, and slower and more costly ICP analysis may be used to estimate application rates.\| ii. Compute the differences in elemental composition as above, potentially including similar performance enhancements such as normalizing by factors specific to each element, summing across subsets of elements, and computing indices such as the ratio of light REEs to heavy REEs. Such transformed and summed variables for a sample will be referred to generically as ΣITEsample.\| iii. The actual application rate of the sample can be calculated using the following expression: l. In one non-limiting embodiment, the verification methodology to calculate the amount of divalent cations remaining in a control volume relative to the amount predicted by the actual mineral application rate (ARactual) as follows:i. The amount of divalent cations applied (DCapplied) can be calculated by the proven identity of the mineral additive and the actual application rate: where divalent cations are generally restricted in this context to Mg and Ca, and Mgmineral and Camineral is the fractional composition of the mineral additive.\| ii. The amount of divalent cations remaining (DCremain) in the soil could be estimated using the same elemental analysis as previously (if, for example, ICP-MS was used), or determined from the same sample using a different analysis (if, for example XRF was used and Mg was not measured).\| iii. The fractional progress of carbon dioxide removal (CDR) can be estimated by the ratio of remaining divalent cations to applied divalent cations: m. In one non-limiting embodiment, the verification methodology to calculate the amount of carbon dioxide removed from the control volume is as follows:i. Assembling MP, fCDR , ARnominal and the land area applied, the total carbon dioxide removal is: n. While Verification Methodology 2 presented herein provides a broad framework for the detection and application of soil-bound ITEs to estimate long-term geologic carbon drawdown, the efficacy of the approach can also be improved through the focus on specific subsets of ITEs. Non-limiting embodiments of such improvements are listed below:i. The ITEs specified in equation 2, e.g., (ΣITEssoil B), may in fact be represented not by the full summation of 17 REEs but instead by the use of only LREEs or the use of only HREEs, as defined in clause xii. Such a calculation would mean the sum of only LREEs in the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium) or the sum of only HREEs in the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium).\| ii. Within the use of only LREEs for the calculation (yttrium, scandium, lanthanum, cerium, praseodymium, neodymium, promethium, and samarium), some LREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual LREEs are selected. For example, the subset may include three LREEs. The calculation (equation 2) is conducted for each of the 3 LREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 LREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [yttrium, scandium, lanthanum], [cerium, lanthanum, neodymium], [cerium, neodymium, samarium], [yttrium, cerium, neodymium], [scandium, neodymium, samarium].\| iii. Within the use of only HREEs for the calculation (europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium), some HREEs may serve as immobile elements more effectively than others. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual HREEs are selected. For example, the subset may include three HREEs. The calculation (equation 2a) is conducted for each of the 3 HREEs individually, and an average and standard deviation is then reported for the CDR calculation. Among the 3 HREEs, the following triplicates are listed as potential, non-limiting candidates of interest: [europium, gadolinium, terbium], [europium, terbium, dysprosium], [dysprosium, erbium, ytterbium], [europium, erbium, ytterbium], [europium, dysprosium, erbium].\| iv. In order to establish an acceptable average and standard deviation for the C drawdown calculation, a subset of the individual REEs are selected. For example, the subset may include three REEs Chart 1 represents a non-limiting list of REE triplicates that may enhance the efficacy of this C drawdown calculation.Chart 1. A non-limiting list of 455 REE triplicates that can be used to effectively triangulate a C drawdown estimation\|('Y', 'La', 'Ce'), ('Y', 'La', 'Pr'), ('Y', 'La', 'Nd'), ('Y', 'La', 'Sm'), ('Y', 'La', 'Eu'), ('Y', 'La', 'Gd'), ('Y', 'La', 'Tb'), ('Y', 'La', 'Dy'), ('Y', 'La', 'Ho'), ('Y', 'La', 'Er'), ('Y', 'La', 'Tm'), ('Y', 'La', 'Yb'), ('Y', 'La', 'Lu'), ('Y', 'Ce', 'Pr'), ('Y', 'Ce', 'Nd'), ('Y', 'Ce', 'Sm'), ('Y', 'Ce', 'Eu'), ('Y', 'Ce', 'Gd'), ('Y', 'Ce', 'Tb' ), ('Y', 'Ce', 'Dy'), ('Y', 'Ce', 'Ho'), ('Y', 'Ce', 'Er'), ('Y', 'Ce', 'Tm'), ('Y', 'Ce', 'Yb'), ('Y', 'Ce', 'Lu'), (' Y', 'Pr', 'Nd'), ('Y', 'Pr', 'Sm'), ('Y', 'Pr', 'Eu'), ('Y', 'Pr', 'Gd'), ('Y', 'Pr', 'Tb'), ('Y', 'Pr', 'Dy'), ('Y', 'Pr ', 'Ho'), ('Y', 'Pr', 'Er'), ('Y', 'Pr', 'Tm'), ('Y', 'Pr', 'Yb'), ('Y', 'Pr', 'Lu'), ('Y', 'Nd', 'Sm'), ('Y', 'Nd', 'E u'), ('Y', 'Nd', 'Gd'), ('Y', 'Nd', 'Tb'), ('Y', 'Nd', 'Dy'), ('Y', 'Nd', 'Ho'), ('Y', 'Nd', 'Er'), ('Y', 'Nd', 'Tm' ), ('Y', 'Nd', 'Yb'), ('Y', 'Nd', 'Lu'), ('Y', 'Sm', 'Eu'), ('Y', 'Sm', 'Gd'), ('Y', 'Sm', 'Tb'), ('Y', 'Sm', 'Dy'), ('Y', 'Sm', 'Ho'), ('Y', 'Sm', 'Er'), ('Y', 'Sm', 'Tm'), ('Y', 'Sm', 'Yb'), ('Y', 'Sm', 'Lu'), ('Y', 'Eu', 'Gd'), ('Y', 'Eu', 'Tb'), ('Y', 'Eu', 'Dy'), ('Y', 'Eu', 'Ho'), ('Y', 'Eu', 'Er'), ('Y', 'Eu', 'Tm'), ('Y', 'Eu', 'Yb'), ('Y ', 'Eu', 'Lu'), ('Y', 'Gd', 'Tb'), ('Y', 'Gd', 'Dy'), ('Y', 'Gd', 'Ho'), ('Y', 'Gd', 'Er'), ('Y', 'Gd', 'Tm'), ('Y', ' Gd', 'Yb'), ('Y', 'Gd', 'Lu'), ('Y', 'Tb', 'Dy'), ('Y', 'Tb', 'Ho'), ('Y', 'Tb', 'Er'), ('Y', 'Tb', 'Tm'), ('Y', 'Tb ', 'Yb'), ('Y', 'Tb', 'Lu'), ('Y', 'Dy', 'Ho'), ('Y', 'Dy', 'Er'), ('Y', 'Dy', 'Tm'), ('Y', 'Dy', 'Yb'), ('Y', 'Dy', 'Lu'), ('Y', 'Ho', 'Er'), ('Y', 'Ho', 'Tm'), ('Y', 'Ho', 'Yb'), ('Y', 'Ho', 'Lu'), ('Y', 'Er', 'Tm'), ('Y', 'Er', 'Y b'), ('Y', 'Er', 'Lu'), ('Y', 'Tm', 'Yb'), ('Y', 'Tm', 'Lu'), ('Y', 'Yb', 'Lu'), ('La', 'Ce', 'Pr'), ('La', 'Ce', 'Nd' ), ('La', 'Ce', 'Sm'), ('La', 'Ce', 'Eu'), ('La', 'Ce', 'Gd'), ('La', 'Ce', 'Tb'), ('La', 'Ce', 'Dy'), ('La', 'Ce', ' Ho'), ('La', 'Ce', 'Er'), ('La', 'Ce', 'Tm'), ('La', 'Ce', 'Yb'), ('La', 'Ce', 'Lu'), ('La', 'Pr', 'Nd'), ('La', 'Pr', 'Sm'), ('La', 'Pr', 'Eu'), ('La', 'Pr', 'Gd'), ('La', 'Pr', 'Tb'), ('La', 'Pr', 'Dy'), ('La', 'Pr', 'Ho'), ('La', 'Pr', ' Er'), ('La', 'Pr', 'Tm'), ('La', 'Pr', 'Yb'), ('La', 'Pr', 'Lu'), ('La', 'Nd', 'Sm'), ('La', 'Nd', 'Eu'), ('La', 'Nd', 'Gd'), ('La', 'Nd', 'Tb'), ('La', 'Nd', 'Dy'), ('La', 'Nd', 'Ho'), ('La', 'Nd', 'Er'), ('La', 'Nd', 'Tm'), ('La', ' Nd', 'Yb'), ('La', 'Nd', 'Lu'), ('La', 'Sm', 'Eu'), ('La', 'Sm', 'Gd'), ('La', 'Sm', 'Tb'), ('La', 'Sm', 'Dy'), (' La', 'Sm', 'Ho'), ('La', 'Sm', 'Er'), ('La', 'Sm', 'Tm'), ('La', 'Sm', 'Yb'), ('La', 'Sm', 'Lu'), ('La', 'Eu', 'G d'), ('La', 'Eu', 'Tb'), ('La', 'Eu', 'Dy'), ('La', 'Eu', 'Ho'), ('La', 'Eu', 'Er'), ('La', 'Eu', 'Tm'), ('La', 'Eu', ' Yb'), ('La', 'Eu', 'Lu'), ('La', 'Gd', 'Tb'), ('La', 'Gd', 'Dy'), ('La', 'Gd', 'Ho'), ('La', 'Gd', 'Er'), ('La', 'G d', 'Tm'), ('La', 'Gd', 'Yb'), ('La', 'Gd', 'Lu'), ('La', 'Tb', 'Dy'), ('La', 'Tb', 'Ho'), ('La', 'Tb', 'Er'), ('La', 'Tb', 'Tm'), ('La', 'Tb', 'Yb'), ('La', 'Tb', 'Lu'), ('La', 'Dy', 'Ho'), ('La', 'Dy', 'Er'), ('La', 'Dy', 'Tm'), ('L a', 'Dy', 'Yb'), ('La', 'Dy', 'Lu'), ('La', 'Ho', 'Er'), ('La', 'Ho', 'Tm'), ('La', 'Ho', 'Yb'), ('La', 'Ho', 'Lu'), ('La', 'Er', 'Tm'), ('La', 'Er', 'Yb'), ('La', 'Er', 'Lu'), ('La', 'Tm', 'Yb'), ('La', 'Tm', 'Lu'), ('La', 'Yb', 'Lu' ), ('Ce', 'Pr', 'Nd'), ('Ce', 'Pr', 'Sm'), ('Ce', 'Pr', 'Eu'), ('Ce', 'Pr', 'Gd'), ('Ce', 'Pr', 'Tb'), ('Ce', 'Pr', 'Dy' ), ('Ce', 'Pr', 'Ho'), ('Ce', 'Pr', 'Er'), ('Ce', 'Pr', 'Tm'), ('Ce', 'Pr', 'Yb'), ('Ce', 'Pr', 'Lu'), ('Ce', 'Nd', 'Sm '), ('Ce', 'Nd', 'Eu'), ('Ce', 'Nd', 'Gd'), ('Ce', 'Nd', 'Tb'), ('Ce', 'Nd', 'Dy'), ('Ce', 'Nd', 'Ho'), ('Ce', 'Nd', 'Er'), ('Ce', 'Nd', 'Tm'), ('Ce', 'Nd', 'Yb'), ('Ce', 'Nd', 'Lu'), ('Ce', 'Sm', 'Eu'), ('Ce', 'Sm', 'Gd'), ('Ce', ' Sm', 'Tb'), ('Ce', 'Sm', 'Dy'), ('Ce', 'Sm', 'Ho'), ('Ce', 'Sm', 'Er'), ('Ce', 'Sm', 'Tm'), ('Ce', 'Sm', 'Yb'), ('Ce', 'Sm', 'Lu'), ('Ce', 'Eu', 'Gd'), ('Ce', 'Eu', 'Tb'), ('Ce', 'Eu', 'Dy'), ('Ce', 'Eu', 'Ho'), ('Ce', 'Eu', 'Er '), ('Ce', 'Eu', 'Tm'), ('Ce', 'Eu', 'Yb'), ('Ce', 'Eu', 'Lu'), ('Ce', 'Gd', 'Tb'), ('Ce', 'Gd', 'Dy'), ('Ce', 'Gd', 'Ho'), ('Ce', 'Gd', 'Er'), ('Ce', 'Gd', 'Tm'), ('Ce', 'Gd', 'Yb'), ('Ce', 'Gd', 'Lu'), ('Ce', 'Tb', 'Dy'), ('Ce', ' Tb', 'Ho'), ('Ce', 'Tb', 'Er'), ('Ce', 'Tb', 'Tm'), ('Ce', 'Tb', 'Yb'), ('Ce', 'Tb', 'Lu'), ('Ce', 'Dy', 'Ho'), ('C e', 'Dy', 'Er'), ('Ce', 'Dy', 'Tm'), ('Ce', 'Dy', 'Yb'), ('Ce', 'Dy', 'Lu'), ('Ce', 'Ho', 'Er'), ('Ce', 'Ho', 'Tm'), ('Ce', 'Ho', 'Yb'), ('Ce', 'Ho', 'Lu'), ('Ce', 'Er', 'Tm'), ('Ce', 'Er', 'Yb'), ('Ce', 'Er', 'Lu'), ('Ce', 'Tm', ' Yb'), ('Ce', 'Tm', 'Lu'), ('Ce', 'Yb', 'Lu'), ('Pr', 'Nd', 'Sm'), ('Pr', 'Nd', 'Eu'), ('Pr', 'Nd', 'Gd'), ('Pr', 'N d', 'Tb'), ('Pr', 'Nd', 'Dy'), ('Pr', 'Nd', 'Ho'), ('Pr', 'Nd', 'Er'), ('Pr', 'Nd', 'Tm'), ('Pr', 'Nd', 'Yb'), ('Pr', ' Nd', 'Lu'), ('Pr', 'Sm', 'Eu'), ('Pr', 'Sm', 'Gd'), ('Pr', 'Sm', 'Tb'), ('Pr', 'Sm', 'Dy'), ('Pr', 'Sm', 'Ho'), ('Pr ', 'Sm', 'Er'), ('Pr', 'Sm', 'Tm'), ('Pr', 'Sm', 'Yb'), ('Pr', 'Sm', 'Lu'), ('Pr', 'Eu', 'Gd'), ('Pr', 'Eu', 'Tb'), (' Pr', 'Eu', 'Dy'), ('Pr', 'Eu', 'Ho'), ('Pr', 'Eu', 'Er'), ('Pr', 'Eu', 'Tm'), ('Pr', 'Eu', 'Yb'), ('Pr', 'Eu', 'Lu'), (' Pr', 'Gd', 'Tb'), ('Pr', 'Gd', 'Dy'), ('Pr', 'Gd', 'Ho'), ('Pr', 'Gd', 'Er'), ('Pr', 'Gd', 'Tm'), ('Pr', 'Gd', 'Yb'), ('Pr', 'Gd', 'Lu'), ('Pr', 'Tb', 'Dy'), ('Pr', 'Tb', 'Ho'), ('Pr', 'Tb', 'Er'), ('Pr', 'Tb', 'Tm'), ('Pr', 'Tb', 'Yb'), ('Pr', 'Tb', 'Lu'), ('Pr', 'Dy', 'Ho'), ('Pr', 'Dy', 'Er'), ('Pr', 'Dy', 'Tm'), ('Pr', 'Dy', 'Yb'), ('Pr', 'Dy', 'Lu'), ('Pr', 'Ho', 'Er'), ('Pr', 'Ho', 'Tm'), ('Pr', 'Ho', 'Yb'), ('Pr', 'Ho', 'Lu'), ('Pr', 'Er', 'Tm'), ('Pr', 'Er', 'Yb'), ('Pr', 'Er', 'Lu'), ('Pr', 'Tm', 'Yb'), ('Pr', 'Tm', 'Lu'), ('Pr', 'Yb', 'Lu'), ('Nd', 'Sm', 'Eu'), ('Nd', 'Sm', 'Gd '), ('Nd', 'Sm', 'Tb'), ('Nd', 'Sm', 'Dy'), ('Nd', 'Sm', 'Ho'), ('Nd', 'Sm', 'Er'), ('Nd', 'Sm', 'Tm'), ('Nd', ' Sm', 'Yb'), ('Nd', 'Sm', 'Lu'), ('Nd', 'Eu', 'Gd'), ('Nd', 'Eu', 'Tb'), ('Nd', 'Eu', 'Dy'), ('Nd', 'Eu', 'Ho'), (' Nd', 'Eu', 'Er'), ('Nd', 'Eu', 'Tm'), ('Nd', 'Eu', 'Yb'), ('Nd', 'Eu', 'Lu'), ('Nd', 'Gd', 'Tb'), ('Nd', 'Gd', 'D y'), ('Nd', 'Gd', 'Ho'), ('Nd', 'Gd', 'Er'), ('Nd', 'Gd', 'Tm'), ('Nd', 'Gd', 'Yb'), ('Nd', 'Gd', 'Lu'), ('Nd', ' Tb', 'Dy'), ('Nd', 'Tb', 'Ho'), ('Nd', 'Tb', 'Er'), ('Nd', 'Tb', 'Tm'), ('Nd', 'Tb', 'Yb'), ('Nd', 'Tb', 'Lu'), (' Nd', 'Dy', 'Ho'), ('Nd', 'Dy', 'Er'), ('Nd', 'Dy', 'Tm'), ('Nd', 'Dy', 'Yb'), ('Nd', 'Dy', 'Lu'), ('Nd', 'Ho', ' Er'), ('Nd', 'Ho', 'Tm'), ('Nd', 'Ho', 'Yb'), ('Nd', 'Ho', 'Lu'), ('Nd', 'Er', 'Tm'), ('Nd', 'Er', 'Yb'), ('Nd', ' Er', 'Lu'), ('Nd', 'Tm', 'Yb'), ('Nd', 'Tm', 'Lu'), ('Nd', 'Yb', 'Lu'), ('Sm', 'Eu', 'Gd'), ('Sm', 'Eu', 'Tb'), ( 'Sm', 'Eu', 'Dy'), ('Sm', 'Eu', 'Ho'), ('Sm', 'Eu', 'Er'), ('Sm', 'Eu', 'Tm'), ('Sm', 'Eu', 'Yb'), ('Sm', 'Eu', ' Lu'), ('Sm', 'Gd', 'Tb'), ('Sm', 'Gd', 'Dy'), ('Sm', 'Gd', 'Ho'), ('Sm', 'Gd', 'Er'), ('Sm', 'Gd', 'Tm'), ('Sm ', 'Gd', 'Yb'), ('Sm', 'Gd', 'Lu'), ('Sm', 'Tb', 'Dy'), ('Sm', 'Tb', 'Ho'), ('Sm', 'Tb', 'Er'), ('Sm', 'Tb', 'Tm' ), ('Sm', 'Tb', 'Yb'), ('Sm', 'Tb', 'Lu'), ('Sm', 'Dy', 'Ho'), ('Sm', 'Dy', 'Er'), ('Sm', 'Dy', 'Tm'), ('Sm', 'D y', 'Yb'), ('Sm', 'Dy', 'Lu'), ('Sm', 'Ho', 'Er'), ('Sm', 'Ho', 'Tm'), ('Sm', 'Ho', 'Yb'), ('Sm', 'Ho', 'Lu'), (' Sm', 'Er', 'Tm'), ('Sm', 'Er', 'Yb'), ('Sm', 'Er', 'Lu'), ('Sm', 'Tm', 'Yb'), ('Sm', 'Tm', 'Lu'), ('Sm', 'Yb', ' Lu'), ('Eu', 'Gd', 'Tb'), ('Eu', 'Gd', 'Dy'), ('Eu', 'Gd', 'Ho'), ('Eu', 'Gd', 'Er'), ('Eu', 'Gd', 'Tm'), ('Eu', ' Gd', 'Yb'), ('Eu', 'Gd', 'Lu'), ('Eu', 'Tb', 'Dy'), ('Eu', 'Tb', 'Ho'), ('Eu', 'Tb', 'Er'), ('Eu', 'Tb', 'Tm'), ('E u', 'Tb', 'Yb'), ('Eu', 'Tb', 'Lu'), ('Eu', 'Dy', 'Ho'), ('Eu', 'Dy', 'Er'), ('Eu', 'Dy', 'Tm'), ('Eu', 'Dy', 'Yb'), ('Eu', 'Dy', 'Lu'), ('Eu', 'Ho', 'Er'), ('Eu', 'Ho', 'Tm'), ('Eu', 'Ho', 'Yb'), ('Eu', 'Ho', 'Lu'), ('Eu', 'Er', 'T m'), ('Eu', 'Er', 'Yb'), ('Eu', 'Er', 'Lu'), ('Eu', 'Tm', 'Yb'), ('Eu', 'Tm', 'Lu'), ('Eu', 'Yb', 'Lu'), ('Gd', 'Tb ', 'Dy'), ('Gd', 'Tb', 'Ho'), ('Gd', 'Tb', 'Er'), ('Gd', 'Tb', 'Tm'), ('Gd', 'Tb', 'Yb'), ('Gd', 'Tb', 'Lu'), ('Gd', 'Dy', 'Ho'), ('Gd', 'Dy', 'Er'), ('Gd', 'Dy', 'Tm'), ('Gd', 'Dy', 'Yb'), ('Gd', 'Dy', 'Lu'), ('Gd', 'Ho', 'Er'), ('Gd', 'Ho', 'Tm'), ('Gd', 'Ho', 'Yb'), ('Gd', 'Ho', 'Lu'), ('Gd', 'Er', 'Tm'), ('Gd', 'Er', 'Yb'), ('Gd', 'Er', ' Lu'), ('Gd', 'Tm', 'Yb'), ('Gd', 'Tm', 'Lu'), ('Gd', 'Yb', 'Lu'), ('Tb', 'Dy', 'Ho'), ('Tb', 'Dy', 'Er'), ('Tb', ' Dy', 'Tm'), ('Tb', 'Dy', 'Yb'), ('Tb', 'Dy', 'Lu'), ('Tb', 'Ho', 'Er'), ('Tb', 'Ho', 'Tm'), ('Tb', 'Ho', 'Yb'), (' Tb', 'Ho', 'Lu'), ('Tb', 'Er', 'Tm'), ('Tb', 'Er', 'Yb'), ('Tb', 'Er', 'Lu'), ('Tb', 'Tm', 'Yb'), ('Tb', 'Tm', 'Lu' ), ('Tb', 'Yb', 'Lu'), ('Dy', 'Ho', 'Er'), ('Dy', 'Ho', 'Tm'), ('Dy', 'Ho', 'Yb'), ('Dy', 'Ho', 'Lu'), ('Dy', 'Er', 'Tm'), ('Dy', 'Er', 'Yb'), ('Dy', 'Er', 'Lu'), ('Dy', 'Tm', 'Yb'), ('Dy', 'Tm', 'Lu'), ('Dy', 'Yb', 'Lu'), ('Ho', 'Er', 'Tm'), ('Ho', 'Er', 'Yb'), ('Ho', 'Er', 'Lu'), ('Ho', 'Tm', 'Yb'), ('Ho', 'Tm', 'Lu'), ('Ho', 'Yb', 'Lu'), (' Er', 'Tm', 'Yb'), ('Er', 'Tm', 'Lu'), ('Er', 'Yb', 'Lu'), ('Tm', 'Yb', 'Lu') 3. Example Verification methodology 3: this methodology expands on Verification methodology 2 by the use of naturally occurring microbial cation exchangers, including bacteria and fungi.i. As above but right before step vii (unsealing samples in laboratory), add the following steps:\| ii. Lyse the microbes. For example, autoclave each sample-containing beaker for steam sterilization at 250 °F at 15 psi for 15 minutes. This may lyse any microbes and cause an active release of bio-adsorbed metals.\| iii. Let sample-containing beakers cool to room temperature before proceeding.\| iv. The filter in step (ix) may now act to additionally remove any larger aggregates of microbial cell suspensions that did not lyse in the autoclaving process.\| v. The added EDTA in step (x) in Verification Methodology 2 may act to additionally chelate any REEs that are complexed to the cell wall or organic molecules of the microbial genetic material (as a result of cell lysis).\| vi. In conjunction, verification methodology 3 provides a protocol to achieve full recovery of REEs that were retained in the top 10 cm of soil due to the following biogeochemical processes:1. Mineral surface interface complexation.\| 2. The cation exchange capacity inherent to soils due to organic matter.\| 3. Microbially mediated surface biosorption and/or active biological absorption pathways including but not limited to REE-aqueous complexation with internal genetic material of individual microbial cells found in natural soils and sediments. B. Example systems and methods to enhance the agronomic performance and ecosystem co-benefits:In these non-limiting embodiments, product formulations are detailed that improve the soil quality for improved agronomic applications as well as embodiments that specify improvements on crop health and an ability for plants to protect themselves from pathogens.\| Addition of macronutrients that enhance the agronomic benefits of the applied mineral. Example: addition of elemental 1-5% by weight formulation K or Ca or inexpensive REE such as La to improve use cases of pulverized Mg2SiO4 by improving the nutrient balance of the soil to match the needs of actively growing plants. Application rates for K and Ca may range from 50-100 ppm and lanthanide addition rates may range from 1-50 ppm.\| The 1-5% by volume addition of slow-release acidifiers in the form of elements that maintain the acidity of the soil despite the tendency of the applied mineral to reduce soil acidity in the weathering process. Example: addition of minerals with Al (such as gibbsite, Al(OH)3) or S (such as gypsum, CaSO4)-2H2O), in a rate of 1-10% by weight of total formulation, which contribute to maintaining soil acidity, and thus maintain high rates of weathering, which counteracts the tendency of forsterite weathering to increase alkalinity, which slows rates of weathering.\| The incorporation of additional micronutrients such as zinc (1-5% by weight compared to mineral amendment) to reduce ecosystem losses of phosphorus and downstream ecosystem impacts of phosphate-based fertilizers, such as eutrophication. Phosphates are immobilized via precipitation reactions with the additional zinc metal, so zinc addition slows the transport and reduces mobility of phosphate in the subsoil. As a consequence, phosphate-based fertilizer applications can be performed more safely and with higher confidence that downstream waterways will not form algal blooms and lead to anoxic, uninhabitable waterways for aquatic life. The addition of 1-32 tons/hectare of mineral in conjunction with 1-5% by weight zinc in fields with heavy phosphate application reduces the likelihood of significant phosphate leaching. This also increases nutrient use efficiency, which reduces fertilizer cost to farmers and reduces negative environmental impacts to society. Specifically, phosphate-zinc precipitates become slow-releasing over time due to their immobilization in the soil as a solid phase. This provides longer timeframes for plants to access the phosphate application, reducing the frequency of fertilization.\| The method of mixing of different mineral adjuvants to the primary mineral used for carbon removal can be varied, with impacts on performance. In some embodiments, the admixture (e.g., of gypsum and forsterite) could be completely emulsified. In some embodiments, a nutrient, such as urea, could represent a core that is subsequently coated with a shell of silicate mineral used for carbon removal. In some embodiments the silicate mineral could be the core, and the nutrient, such as urea, could be the coating. In each of these cases, the embodiment can be optimized so as to reduce environmental losses of the nutrient, and increase availability to the plant, while providing the acidity necessary for the silicate mineral weathering. In some embodiments, this may represent a "slow release" nutrient that does not mineralize too quickly and is synchronized more favorably with plant demand.\| Comminution, or pulverization, may help reproduce the expected kinetics of alkalizers such as pulverized limestone or dolomite, known as aglime. Aglime has well-characterized kinetics originating in the particle size distribution of the product, which are in some jurisdictions legally regulated to meet certain requirements. A representative cross section of dissolution kinetics based on actual aglime mesh size observations is depicted in FIG. 2.\|It naturally follows that agronomic performance expectations for silicate minerals used for ERW should follow similar reaction kinetics, particularly in the first year after application, while also meeting the goals for CDR. Thus, an ideal particle size distribution may be tuned to meet this goal. The following shows the kinetics for a particle size distribution of a pulverized silicate with median particle size of 80-100um, such as 90um, which closely approximates the alkalinity release dynamics for aglime.\| The small particle sizes produced by pulverization as above are valuable for performance as an aglime substitute and CDR mechanism, but introduce their own set of potential challenges. One potential challenge is that small particle sizes may fall within regulated categories such as PM10 or PM2.5; another potential challenge is the product may not be easily transferred from one vessel to another (so-called "flowability") because it has a tendency to settle into a compact mass; the product may also not be applied uniformly by extant farm equipment; potentially low uniformity application impacts the agronomic performance as well as the sampling density needed for carbon removal verification. In one potential formulation, the product is pelletized after pulverization, using a common binder such as lignosulfate in a 3-5% ratio by weight of the total formulation. The amount of binder may be optimized to improve performance characteristics during transport and application, but minimize the water and energy needed to dissolve the pellet once it is in the field. Pelletizing the product, into a size range of, for example, 0.5 mm to 3 mm increases the flowability; reduces the prevalence of dust, including the risk of asbestos exposure; enables the use of extant crop input application equipment; and improves the evenness of field distribution, which has the agronomic and carbon verification benefits identified. Pelletizing in this size range also ensures that an adequate number of pellets fall onto any land area which may subsequently be sampled for analysis.\| A desiccated but living biological compound, such as a mycorrhizal inoculum, may be used to coat the agglomerated and dried pellets, so as to enhance the dissolution of the pellet itself after application. This may be distinct from a fungal adjuvant to the pellet to increase dissolution of the silicate minerals themselves.\| To accommodate a range of soil types from acidic to neutral pH, the product may be differentiated into different particle size distributions so as to achieve a consistent rate of weathering across different soil types. For example a consistent rate of weathering may be that the entire applied amount of mineral product weathers in 9 months, allowing a subsequent application every year. To achieve this, an acidic soil may have pellets that contain particles with a modal size on the order of 100 um, while a neutral soil may have pellets that contain particles with a modal size on the order of 10 um. The negative consequence of applying a fine particle in an acidic soil may be that it dissolves too quickly, swinging the pH of the soil too quickly, and altering the nutrient availability severely in the growing plant. The negative consequence of applying a coarse particle in a neutral soil may be that the particle weathers too slowly or is functionally inert, which does not remove carbon as intended, and may subject the farmer or the vendor to risk of clawbacks for payments received for carbon removal. C. Example systems and methods to control or enhance the performance as a securitized carbon removal method:In these non-limiting embodiments, product formulations are described that improve the marketability of pulverized and optionally pelletized mineral amendments as a verifiable carbon removal method, irrespective of their impact on agronomic performance. Such changes in marketability increase the value of the carbon product, for example for detecting and preventing fraud, or increase the dissolution rate (mass per area per year) to accelerate the timing of reapplication, which raises the value in a discounted cash flow analysis. The general scheme is depicted in FIG. 4.\| The addition of low cost and inert trace elements, for example 1-5 ppm neodymium or lanthanum, to a mineral amendment, beyond the natural abundances present in the ore body, improves performance in Verification methods 2 and 3. Specifically, the additional elements reduce measurement uncertainty owing to low natural abundance calculations as well as uncertainty owing to variability from the source mineral. Reduction of these uncertainties improves the detectability of true positives and true negatives. This principle could be applied to many potential soil amendments and fertilizers to verify provenance as pertains to legal contracts.\| The addition of binders to create aggregations of the ground mineral that could reduce drift, which improves distribution uniformity; reduces potential respiratory health impacts; and/or improves applicability of the applied mineral using commercially available equipment. For example, a biofilm mediating organic compound, such as alginate or chitosan, could be mixed with a pulverized mineral with a particle size of approximately 100 microns to achieve an aggregated pellet size of 1 millimeter. This would maintain the advantages of fine particle size, particularly the high specific surface area (m2/g) that mediates dissolution rate, while offsetting potential limitations outlined above. An example methodology for aggregating ground minerals could include these steps:∘ Dissolve 10 grams of alginate powder into solution to create a 0.5 M - 1.0 M alginic acid solution.\| ∘ Heat solution to 80-100 °F to dissolve alginate powder fully if necessary.\| ∘ Spray aerosol sized particles of dissolved alginate powder onto the ground rock material in order to create a biofilm-coated rock material. Apply a consistent spray of 100 mL for each 100 gram of rock (1:1 v/w).\| ∘ The resulting aggregates may have increased bulk density as well as higher aggregating properties due to van der Waals force attraction between the individual rock particles. Dissolution rates can be modified by non-living organic molecules applied concurrently with the mineral amendment. For example, protonated microbes such as acid-treated Arthrobacter nicotianae can constitute an initial release of protons to attack the ground rock materials' crystal structure. This method of acidification for optimal accelerated weathering of rock material may occur even during winter/cold climate. Because biologically mediated processes can have sharp thresholds, e.g., under freezing conditions, such a chemically controlled process would exhibit greater ability to expedite rock breakdown over a range of environmental conditions. To implement this methodology, we outline the following steps:1) De-frost an aliquot of A. nicotianae in 5 mL of Luria broth for about 24 hours at exactly 30 °C.\| 2) Sub-culture into a larger volume of Luria broth at a 1:50 dilution and allow growth for another 24 hours at 30 °C.\| 3) During growth steps #1 and 2, cultures may be shaken, for example at 200-220 RPM, for aeration.\| 4) After culture has been grown for 48 hours in total, centrifuge the cell suspension.\| 5) Collect cell pellet and take a small amount and set it aside. Weigh wet weight, dry at 60 °C overnight, and weigh dry amount to obtain wet : dry conversion.\| 6) Develop an OD600 to wet weight to dry weight conversion by taking 5 varying amounts of wet aliquots of wet biomass and measuring optical density given its known wet mass. Wet aliquots may have a mass of about 1, 4, 8, 12, 16 wet grams and be suspended in 100 mL of DI water.\| 7) Wash cells in 0.1 M NaCl solution.a. Centrifuge cells+growth media at 4000xg.\| b. Carefully pour out LB broth.\| c. Add 0.1 M NaCl solution.\| d. Centrifuge cells+NaCl solution at 4000xg.\| e. Carefully pour out NaCl solution. 8) Protonate the cells while wet.a. Re-suspend the wet biomass in an acidic (e.g., pH 3.0) solution using a dilute hydrochloric acid solution (0.001-0.01 M).\| b. Centrifuge cells+HCl solution at 4000xg.\| c. Carefully pour out solution.\| d. Repeat steps (a)-(c) a total of three times.\| e. Dry cells in an oven at 80-100 °C for 48 hours.\| f. Grind cells using a mortar/pestle to achieve a powder form. 9) Mix 5% w/w of dry cell powder with the ground rock material.\| 10) When this particular rock material+cell powder mixture is applied to agricultural soils, the irrigation or rainfall will re-apply moisture and allow the pre-protonated, re-wet biomass to release their protons. This will ultimately induce a local acidity effect on the rock particle (molecular) level to accelerate rock crystal lattice breakdown. The cells act as biodegradable transporters that are also benign to the natural soil environment.	Family Number\|(103013820)\|103013820\|Object of Invention\|(US11644454 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20220404329 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(WO2022271842 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20230273174 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US11921098 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(EP4276752 A2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(EP4276752 A3)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20240264139 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US12422425 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20260016458 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|Abstract\|(US11644454 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(WO2022271842 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(AU2022299180 A9)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.(From EP4276752 A3)\|(CA3207124 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US11921098 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(EP4256520 C0)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(EP4276752 A3)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(BR112023023226 B1)\|verification methods and agronomic enhancements for carbon removal based on improved weathering of rocks. this description refers to methods to verify improved weathering of rocks using traces of immovable elements found within a mineral correction. mineral corrections that allow for improved weathering of rocks are also described\|(US12422425 B2)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|(US20260016458 A1)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.\|Title\|(US11644454 B2)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US20220404329 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(WO2022271842 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(AU2022299180 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(AU2022299180 A9)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(CA3207124 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US20230273174 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US11921098 B2)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4256520 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4256520 A4)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4256520 B1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4256520 C0)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4276752 A2)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(EP4276752 A3)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(BR112023023226 A0)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(BR112023023226 A2)\|Verification methods and agronomic improvements for carbon removal based on improved rock weathering\|(BR112023023226 B1)\|Method to verify enhanced rock weathering using a mineral correction\|(US20240264139 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US12422425 B2)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(HK40094979 A)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(HK40095252 A)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|(US20260016458 A1)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering\|Advantages / Prev. Drawbacks\|(US20220404329 A1)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(CA3207124 A1)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(US20230273174 A1)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(US11921098 B2)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(EP4276752 A2)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|(US20240264139 A1)\|The potential for ERW as a commercial enterprise is limited by some fundamental issues: A. The total amounts of mineral transformation and carbon removal should be verifiable empirically.\|Independent Claims\|(US11644454 B2)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring (...) \|(US20220404329 A1)\| (...) A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring (...) \| (...) A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(WO2022271842 A1)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring (...) \|12. A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(CA3207124 A1)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: measuring one or more immobile trace elements in a mineral amendment, the immobile trace elements comprising one or more rare earth elements, rare metals, or transition metals; and subsequently measuring (...) \|12. A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(US20230273174 A1)\| (...) A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(US11921098 B2)\|1. A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(EP4256520 B1)\|1. A method for verifying enhanced rock weathering using a mineral amendment comprising: (...) determining the fractional carbon dioxide removal by comparing the applied divalent cations to the measured divalent cations in the soil sample.\|(EP4276752 A2)\|1. A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral having an average particle size of about 0.5 mm to about 3 mm, the agglomerated silicate mineral comprising a comminuted silicate mineral and a binder; and immobile trace elements, the immobile trace (...) \|(US20240264139 A1)\| (...) A mineral amendment for enhanced rock weathering comprising: an agglomerated silicate mineral comprising a comminuted silicate mineral and a binder, the comminuted silicate mineral having an average particle size between about 80 μm and about 100 μm; and immobile trace elements, the immobile (...) \|(US12422425 B2)\|1. A mineral amendment for enhanced rock weathering comprising: (...) \|(US20260016458 A1)\| (...) A method for verifying enhanced rock weathering using a mineral amendment comprising: (...) \|	Analysis of biological materials\|Basic materials chemistry\|Computer technology\|Electrical machinery, apparatus, energy\|Environmental technology\|Telecommunications	B01D-053/62\|B01D-2253/106\|B01D-2253/304\|B01D-2257/504\|C09K-011/77\|C09K-017/00\|C09K-017/12\|G01N-033/24\|H01J-049/10/5\|Y02C-020/40		B01D-053/62\|B01D-2253/106\|B01D-2253/304\|B01D-2257/504\|C09K-011/77\|C09K-017/00\|C09K-017/12\|G01N-033/24\|H01J-049/10/5\|Y02C-020/40	B01D-053/34\|B01D-053/62\|C09K-011/77\|C09K-017/00\|C09K-017/12\|G01N-033/24\|G06T-007/00\|G06T-007/60\|G16C-020/20\|G16C-020/70\|H01J-049/10	B01D-053/34\|B01D-053/62\|C09K-011/77\|C09K-017/00\|C09K-017/12\|G01N-033/24\|G06T-007/00\|G06T-007/60\|G16C-020/20\|G16C-020/70\|H01J-049/10			WO2024156029\|US20240383758\|US12422425	WO2024156029 110849874 WHO=Examiner SELF=N CAT=X\|US20240383758 112187058 WHO=Examiner SELF=N CAT=103\|US12422425 103013820 WHO=Examiner SELF=Y	US20210144935\|US20210144935\|US20210144935\|JP07088362\|US11921098\|US20220065103\|US20210144935\|US20190086381\|US20180082794\|US6753957\|US3864140\|US3853573\|US3856545	US20210144935 94130659 WHO=Examiner SELF=N CAT=A\|US20210144935 94130659 WHO=Examiner SELF=N CAT=A\|US20210144935 94130659 WHO=Examiner SELF=N CAT=A\|JP07088362 24293047 WHO=Examiner SELF=N CAT=A\|US11921098 103013820 WHO=Examiner SELF=Y\|US20220065103 98850983 WHO=Examiner SELF=N\|US20210144935 94130659 WHO=Applicant SELF=N\|US20190086381 83774390 WHO=Examiner SELF=N\|US20180082794 79099270 WHO=Examiner SELF=N\|US6753957 43373580 WHO=Examiner SELF=N\|US3864140 42244845 WHO=Examiner SELF=N\|US3853573 42252986 WHO=Examiner SELF=N\|US3856545 42260687 WHO=Examiner SELF=N		\|US11921098\|\|US3853573; US3856545; US3864140\|XP093021187; XP093021188; XP086574323; XP093021190; US20210144935\|\|\|US20210144935; XP086574323; XP093052931; XP093207104; XP085383712\|US20210144935; XP086574323; JP07088362; XP055822446\|\|\|US6753957; US20180082794; US20190086381; US20220065103; US20210144935	(EP4256520)\|Search Report references [Examiner]\|-PAULO CARLOS ET AL: "Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 129, 6 April 2021 (2021-04-06), XP086574323, ISSN: 0883-2927, [retrieved on 20210406], DOI: 10.1016/J.APGEOCHEM.2021.104955\|-MOOSDORF NILS ET AL: "Carbon Dioxide Efficiency of Terrestrial Enhanced Weathering", ENVIRONMENTAL SCIENCE & TECHNOLOGY, vol. 48, no. 9, 8 April 2014 (2014-04-08), US, pages 4809 - 4816, XP093052931, ISSN: 0013-936X, DOI: 10.1021/es4052022\|-LIU PU-LING ET AL: "Stable rare earth element tracers to evaluate soil erosion", SOIL AND TILLAGE RESEARCH, vol. 76, no. 2, 1 April 2004 (2004-04-01), NL, pages 147 - 155, XP093207104, ISSN: 0167-1987, DOI: 10.1016/j.still.2003.09.005\|-See also references of WO 2022271842A1\|-POTORT� ANGELA GIORGIA ET AL: "Traceability of Protected Geographical Indication (PGI) Interdonato lemon pulps by chemometric analysis of the mineral composition", JOURNAL OF FOOD COMPOSITION AND ANALYSIS, ELSEVIER, AMSTERDAM, NL, vol. 69, 15 March 2018 (2018-03-15), pages 122 - 128, XP085383712, ISSN: 0889-1575, DOI: 10.1016/J.JFCA.2018.03.001\|-C. Paulo et al, Applied Geochemistry, 2021, 219, 104955\|-N. Moosdorf et al, Environ. Sci. Tech., 2014, 48, 4809\|\|(EP4276752)\|Applicant references\|-PAULO CARLOS ET AL: "Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 129, 6 April 2021 (2021-04-06), XP086574323, ISSN: 0883-2927, [retrieved on 20210406], DOI: 10.1016/J.APGEOCHEM.2021.104955\|-SANNA A. ET AL: "A review of mineral carbonation technologies to sequester CO 2", CHEMICAL SOCIETY REVIEWS, vol. 43, no. 23, 1 January 2014 (2014-01-01), UK, pages 8049 - 8080, XP055822446, ISSN: 0306-0012, DOI: 10.1039/C4CS00035H\|\|(US12422425)\|Examiner references\|\|\|(US11644454)\|Applicant references\|-Haque et al. “Alkaline Mineral Soil Amendment: A Climate Change ‘Stabilization Wedge’?” Energies. 2019; 12 (12):2299. https://doi.org/10.3390/en12122299, Abstract; p. 8, para 2, 3.\|-Haque et al. “Risk assessment of Nl, Cr, and Si release from alkaline minerals during enhanced weathering” Open Agriculture, vol. 5, No. 1, 2020, doi: https://doi.org/10.1515/opag-2020-0016, Abstract; p. 167 para 4-p. 168 para 1; p. 169, para 2.\|-Paulo et al. “Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization.” Applied Geochemistry. Apr. 6, 2021, 129. 104955. 10.1016/j.apgeochem.2021. 104955. entire document.\|-Strefler et al. (2018). “Potential and costs of carbon dioxide removal by enhanced weathering of rocks.” Environmental Research Letters. 13. 10.1088/1748-9326/aaa9c4. entire document.\|-International Search Report and Written Opinion of the International Searching Authority for International Patent App. No. PCT/US22/34546 dated Nov. 15, 2022. (10 pages).\|\|\|(WO2022/271842)\|International Search Report [Examiner]\|-HAQUE FATIMA, CHIANG YI, SANTOS RAFAEL: "Alkaline Mineral Soil Amendment: A Climate Change ‘Stabilization Wedge’?", ENERGIES, vol. 12, no. 12, pages 2299, XP093021187, DOI: 10.3390/en12122299\|-HAQUE FATIMA, CHIANG YI WAI, SANTOS RAFAEL M.: "Risk assessment of Ni, Cr, and Si release from alkaline minerals during enhanced weathering", OPEN AGRICULTURE, vol. 5, no. 1, 1 January 2020 (2020-01-01), pages 166 - 175, XP093021188, DOI: 10.1515/opag-2020-0016\|-PAULO CARLOS; POWER IAN M.; STUBBS AMANDA R.; WANG BAOLIN; ZEYEN NINA; WILSON SIOBHAN A.: "Evaluating feedstocks for carbon dioxide removal by enhanced rock weathering and CO2 mineralization", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 129, 6 April 2021 (2021-04-06), AMSTERDAM, NL , XP086574323, ISSN: 0883-2927, DOI: 10.1016/j.apgeochem.2021.104955\|-GREGORY UPSCALING, NEMET F, CALLAGHAN MAX W, FELIX, STREFLER JESSICA, AMANN THORBEN, BAUER NICO, KRIEGLER ELMAR, HARTMANN JENS: " Potential and costs of carbon dioxide removal by enhanced weathering of rocks", ENVIRONMENTAL RESEARCH LETTERS, 1 January 2018 (2018-01-01), pages 34010, XP093021190, Retrieved from the Internet <URL:https://iopscience.iop.org/article/10.1088/1748-9326/aaa9c4/pdf> [retrieved on 20230206]\|-See also references of EP 4256520A4\|\|\|\|\|\|	GRANTED	(EP4256520)\|GRANTED\|(EP4276752)\|PENDING\|(US12422425)\|GRANTED\|(US11921098)\|GRANTED\|(US11644454)\|GRANTED\|(US20260016458)\|PENDING\|(WO2022/271842)\|LAPSED\|(BR112023023226)\|GRANTED\|(AU2022299180)\|PENDING\|(HK40095252)\|PENDING\|(HK40094979)\|PENDING\|(CA3207124)\|PENDING	ALIVE	(EP4256520)\|ALIVE\|(EP4276752)\|ALIVE\|(US12422425)\|ALIVE\|(US11921098)\|ALIVE\|(US11644454)\|ALIVE\|(US20260016458)\|ALIVE\|(WO2022/271842)\|DEAD\|(BR112023023226)\|ALIVE\|(AU2022299180)\|ALIVE\|(HK40095252)\|ALIVE\|(HK40094979)\|ALIVE\|(CA3207124)\|ALIVE	(EP4256520)\|LEGAL DETAILS FOR EP4256520\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2022-06-22\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP22829238\|Application date=2022-06-22\|Standardized application number=2022EP-0829238\|Event publication date=2022-12-30\|Event code=EP/STAAPCT\|Event group=Examination events Entry into national phase\|The international publication has been made\|Original code: STAA\|Event publication date=2023-09-08\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2023-09-08\|Event code=EP/STAARQ\|Event indicator=Pos\|Event group=Examination events\|Request for examination was made\|Original code: STAA\|Event publication date=2023-10-11\|Event code=EP/A1\|Event 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state=EE\|MEMBER STATE LEGAL DETAILS FOR EP4276752\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP23199092\|Application date in the designated or member state=2022-06-22\|Application number in the designated or member state=2023EP-0199092\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP4276752\|Publication stage code in the designated or member state=A2\|Publication date in the designated or member state=2023-11-15\|Publication number in the designated or member state=EP4276752\|MEMBER STATE LEGAL DETAILS FOR ES\|Actual or expected expiration date=2026-04-10\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=ES\|Event publication date=2026-04-10\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=ES\|MEMBER STATE LEGAL DETAILS FOR FI\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=FI\|Event publication date=2025-12-10\|Event code=FI/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=FI\|MEMBER STATE LEGAL DETAILS FOR FR\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2025-12-10\|Event code=FR/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=FR\|MEMBER STATE LEGAL DETAILS FOR GB\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2025-12-10\|Event code=EP/REG\|Event code=GB/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patent granted\|Corresponding cc:\|Designated or member state=GB\|MEMBER STATE LEGAL DETAILS FOR HK\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=HK Corresponding appl: HK40095252\|Event publication date=2024-01-26\|Event code=EP/REG\|Event code=HK/DE\|Event group=Examination events\|Reference to a national code\|Requests to designate patent in hong kong\|Requests to record published in hong kong\|Corresponding cc:\|Designated or member state=HK\|MEMBER STATE LEGAL DETAILS FOR HR\|Actual or expected expiration date=2026-04-14\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2026-04-14\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=HR\|MEMBER STATE LEGAL DETAILS FOR IE\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2025-12-31\|Event code=EP/REG\|Event code=IE/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patents granted designating Ireland\|European patent granted\|Corresponding cc:\|Designated or member state=IE\|MEMBER STATE LEGAL DETAILS FOR IT\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2025-12-10\|Event code=IT/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=IT\|MEMBER STATE LEGAL DETAILS FOR LT\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2025-12-10\|Event code=LT/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=LT\|MEMBER STATE LEGAL DETAILS FOR LU\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=LU\|Event publication date=2025-12-10\|Event code=LU/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=LU\|MEMBER STATE LEGAL DETAILS FOR LV\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=LV\|Event publication date=2025-12-10\|Event code=LV/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=LV\|MEMBER STATE LEGAL DETAILS FOR MT\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=MT\|Event publication date=2025-12-10\|Event code=MT/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=MT\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2025-12-10\|Event code=NL/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=NL\|MEMBER STATE LEGAL DETAILS FOR NO\|Actual or expected expiration date=2026-04-13\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NO\|Event publication date=2026-04-13\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NO\|MEMBER STATE LEGAL DETAILS FOR PT\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=PT\|Event publication date=2025-12-10\|Event code=PT/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=PT\|MEMBER STATE LEGAL DETAILS FOR RO\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=RO\|Event publication date=2025-12-10\|Event code=RO/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=RO\|MEMBER STATE LEGAL DETAILS FOR SE\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2025-12-10\|Event code=SE/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=SE\|MEMBER STATE LEGAL DETAILS FOR SI\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=SI\|Event publication date=2025-12-10\|Event code=SI/UPCX\|MEMBER STATES COVERED BY UNITARY PATENT PROTECTION\|Corresponding cc:\|Designated or member state=SI\|(EP4276752)\|LEGAL DETAILS FOR EP4276752\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-06-22\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP23199092\|Application date=2022-06-22\|Standardized application number=2023EP-0199092\|Event publication date=2023-10-13\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2023-10-13\|Event code=EP/STAAPB\|Event group=Examination events\|The application has been published\|Original code: STAA\|Event publication date=2023-11-15\|Event code=EP/A2\|Event group=Examination events\|Application published without search report\|Publication country=EP\|Publication number=EP4276752\|Publication stage code=A2\|Publication date=2023-11-15\|Standardized publication number=EP4276752\|Event publication date=2023-11-15\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2024-06-14\|Event code=EP/PUAL\|Event group=Examination events\|SEARCH REPORT DESPATCHED\|Publication of search report\|Original code: 0009013\|Event publication date=2024-07-17\|Event code=EP/A3\|Event indicator=Pos\|Event group=Examination events\|Published search report\|Publication country=EP\|Publication number=EP4276752\|Publication stage code=A3\|Publication date=2024-07-17\|Standardized publication number=EP4276752\|Event publication date=2024-07-17\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2024-07-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2024-07-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2024-07-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2024-07-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2024-07-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2025-01-03\|Event code=EP/STAARQ\|Event indicator=Pos\|Event group=Examination events\|Request for examination was made\|Original code: STAA\|Event publication date=2025-02-05\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2024-12-31\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP4256520\|Event publication date=2023-11-15\|Event code=EP/AC\|Event group=Examination events\|Divisional application: reference to earlier application\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR HK\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=HK Corresponding appl: HK40094979\|Event publication date=2024-01-26\|Event code=EP/REG\|Event code=HK/DE\|Event group=Examination events\|Reference to a national code\|Requests to designate patent in hong kong\|Requests to record published in hong kong\|Corresponding cc:\|Designated or member state=HK\|(US12422425)\|LEGAL DETAILS FOR US12422425\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2024-02-07\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US18435492\|Application date=2024-02-07\|Standardized application number=2024US-18435492\|Event publication date=2024-02-07\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:NGUYEN, KIET TUAN\|Event publication date=2024-02-07\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=2881\|Event publication date=2024-02-07\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 0153961-0782690\|Event publication date=2024-02-07\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 26874\|Event publication date=2024-02-07\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2024-02-07\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2024-02-07\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2024-04-12\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2024-04-15\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2024-04-15\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2024-04-16\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2024-08-08\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20240264139\|Publication stage code=A1\|Publication date=2024-08-08\|Standardized publication number=US20240264139\|Event publication date=2024-08-08\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2024-08-10\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2024-09-07\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2024-09-09\|Event code=US/DBLNF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection - Double Patenting\|RJD=2024-09-09\|R4R=DBL\|RJST=non-final\|Rejected claims 1-10\|RJCT=2009US-11921098\|Event publication date=2024-09-17\|Event code=US/M327\|Event group=Examination events OAO\|Miscellaneous Communication to Applicant - No Action Count\|Event publication date=2024-12-10\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2025-02-12\|Event code=US/CTFR\|Event group=Examination events OA OAO\|Final Rejection\|Event publication date=2025-02-18\|Event code=US/DBLFR\|Event indicator=Neg\|Event group=Examination events\|Final rejection - Double Patenting\|RJD=2025-02-18\|R4R=DBL\|RJST=final\|Rejected claims 1-10\|RJCT=2009US-11921098\|Event publication date=2025-04-11\|Event code=US/INVSUM\|Event group=Examination events OAI INT\|Interview Summary- Applicant Initiated\|Event publication date=2025-04-13\|Event code=US/EXIN\|Event group=Examination events OAO INT\|Examiner Interview Summary Record (PTOL - 413)\|Event publication date=2025-05-27\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2025-05-28\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2025-08-27\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2025-08-27\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2025-08-27\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:WOLF, ADAM;CHANG, ELLIOT SUK-HYUN;TANK, ALAN ROBERT\|Reel/frame:072562/0621\|OWNER:EION CORP., NEW JERSEY\|Effective date of the event=2022-07-22\|Event publication date=2025-08-28\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2025-09-10\|Event code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=2025-09-10\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2025-09-23\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US12422425\|Publication stage code=B2\|Publication date=2025-09-23\|Standardized publication number=US12422425\|Event publication date=2025-09-23\|Event code=US/MEPGNTF\|Event group=Event indicating In Force Administrative notifications\|Mail Patent eGrant Notification\|Event publication date=2025-09-23\|Event code=US/EPGNTF\|Event group=Event indicating In Force Administrative notifications\|Patent eGrant Notification\|Event publication date=2025-09-23\|Event code=US/EPG\|Event group=Event indicating In Force\|Recordation of Patent eGrant\|Event publication date=2025-09-23\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=0\|(US11921098)\|LEGAL DETAILS FOR US11921098\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2023-03-30\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US18128583\|Application date=2023-03-30\|Standardized application number=2023US-18128583\|Event publication date=2023-03-30\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:NGUYEN, KIET TUAN\|Event publication date=2023-03-30\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=2881\|Event publication date=2023-03-30\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 27593-0773011\|Event publication date=2023-03-30\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 26874\|Event publication date=2023-03-30\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2023-03-30\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2023-03-30\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:WOLF, ADAM;CHANG, ELLIOT SUK-HYUN;TANK, ALAN ROBERT\|Reel/frame:063178/0691\|OWNER:EION CORP., NEW JERSEY\|Effective date of the event=2022-07-22\|Event publication date=2023-03-30\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2023-05-03\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2023-05-22\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2023-05-23\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-05-23\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2023-08-31\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20230273174\|Publication stage code=A1\|Publication date=2023-08-31\|Standardized publication number=US20230273174\|Event publication date=2023-08-31\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2023-10-01\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-10-27\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2023-11-01\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2023-11-14\|Event code=US/POAC\|Event group=Change of name or address\|Change in Power of Attorney (May Include Associate POA)\|Event publication date=2024-01-31\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2024-01-31\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2024-02-02\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2024-02-14\|Event code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=2024-02-14\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2024-03-05\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US11921098\|Publication stage code=B2\|Publication date=2024-03-05\|Standardized publication number=US11921098\|Event publication date=2024-03-05\|Event code=US/MEPGNTF\|Event group=Event indicating In Force Administrative notifications\|Mail Patent eGrant Notification\|Event publication date=2024-03-05\|Event code=US/EPGNTF\|Event group=Event indicating In Force Administrative notifications\|Patent eGrant Notification\|Event publication date=2024-03-05\|Event code=US/EPG\|Event group=Event indicating In Force\|Recordation of Patent eGrant\|Event publication date=2024-03-05\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=0\|(US11644454)\|LEGAL DETAILS FOR US11644454\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2022-06-22\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US17846838\|Application date=2022-06-22\|Standardized application number=2022US-17846838\|Event publication date=2022-06-22\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:NGUYEN, KIET TUAN\|Event publication date=2022-06-22\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=2881\|Event publication date=2022-06-22\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 45665-0006\|Event publication date=2022-06-22\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 69082\|Event publication date=2022-06-22\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2022-06-22\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2022-06-22\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2022-06-22\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2022-07-07\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2022-07-08\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2022-08-03\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2022-09-02\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:WOLF, ADAM;CHANG, ELLIOT SUK-HYUN;TANK, ALAN ROBERT\|Reel/frame:060976/0081\|OWNER:EION CORP., NEW JERSEY\|Effective date of the event=2022-07-22\|Event publication date=2022-10-06\|Event code=US/POAC\|Event group=Change of name or address\|Change in Power of Attorney (May Include Associate POA)\|Event publication date=2022-12-16\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2022-12-16\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2022-12-16\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2022-12-22\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20220404329\|Publication stage code=A1\|Publication date=2022-12-22\|Standardized publication number=US20220404329\|Event publication date=2022-12-22\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2023-02-02\|Event code=US/PDPH\|Event group=ACL Examination events\|Petition Decision PPH Decision\|Event publication date=2023-02-06\|Event code=US/PETDGMS\|Event group=ACL\|Record Petition Decision of Granted to Make Special\|Event publication date=2023-02-12\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-03-02\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2023-03-06\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2023-03-10\|Event code=US/ODPD8\|Event group=AMD\|Letter Withdrawing a Notice Requiring Inventor Oath or Declaration\|Event publication date=2023-03-13\|Event code=US/MODPD8\|Event group=Administrative notifications\|Mail Letter Withdrawing a Notice Requiring Inventor Oath or Declaration\|Event publication date=2023-03-29\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2023-03-29\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2023-04-03\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2023-04-19\|Event code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=2023-04-19\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2023-05-09\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US11644454\|Publication stage code=B2\|Publication date=2023-05-09\|Standardized publication number=US11644454\|Event publication date=2023-05-09\|Event code=US/MEPGNTF\|Event group=Event indicating In Force Administrative notifications\|Mail Patent eGrant Notification\|Event publication date=2023-05-09\|Event code=US/EPGNTF\|Event group=Event indicating In Force Administrative notifications\|Patent eGrant Notification\|Event publication date=2023-05-09\|Event code=US/EPG\|Event group=Event indicating In Force\|Recordation of Patent eGrant\|Event publication date=2023-05-09\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=0\|(US20260016458)\|LEGAL DETAILS FOR US20260016458\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-09-22\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19335929\|Application date=2025-09-22\|Standardized application number=2025US-19335929\|Event publication date=2025-09-22\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-09-22\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-09-22\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 0153961-0810853\|Event publication date=2025-09-22\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 26874\|Event publication date=2025-09-22\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2025-09-22\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-09-22\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-09-22\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-10-08\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2025-10-09\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-10-09\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-10-09\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-11-18\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2026-01-15\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20260016458\|Publication stage code=A1\|Publication date=2026-01-15\|Standardized publication number=US20260016458\|Event publication date=2026-01-16\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|(WO2022/271842)\|LEGAL DETAILS FOR WO2022/271842\|Actual or expected expiration date=2024-12-22\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-06-22\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2022/034546\|Application date=2022-06-22\|Standardized application number=2022WO-US34546\|Event publication date=2022-12-29\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2022/271842\|Publication stage code=A1\|Publication date=2022-12-29\|Standardized publication number=WO2022271842\|Event publication date=2024-12-22\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2022299180\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2022299180\|Application date in the designated or member state=2022-06-22\|Application number in the designated or member state=2022AU-0299180\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2022299180\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2023-07-13\|Publication number in the designated or member state=AU2022299180\|Event publication date=2023-07-13\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=AU\|MEMBER STATE LEGAL DETAILS FOR BR112023023226\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=BR Corresponding appl: BR112023023226\|Application date in the designated or member state=2022-06-22\|Application number in the designated or member state=2023BR-0023226\|Corresponding cc:\|Designated or member state=BR Corresponding pat: BR112023023226\|Publication stage code in the designated or member state=A0\|Publication date in the designated or member state=2023-11-14\|Publication number in the designated or member state=BR112023023226\|Event publication date=2023-11-14\|Event code=WO/REG\|Event code=BR/B01A\|Event group=Examination events\|Reference to a national code\|Pct publication - request for entry into the national phase\|Comunicacao da publicacao internacional pct. apresentacao de peticao de requerimento de entrada na fase nacional\|Corresponding cc:\|Designated or member state=BR\|Event publication date=2024-01-30\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2023-11-06\|Corresponding cc:\|Designated or member state=BR\|MEMBER STATE LEGAL DETAILS FOR CA3207124\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA3207124\|Application date in the designated or member state=2022-06-22\|Application number in the designated or member state=2022CA-3207124\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA3207124\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2022-12-29\|Publication number in the designated or member state=CA3207124\|Event publication date=2023-06-29\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2024-01-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2024-01-23\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP4256520\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP22829238\|Application date in the designated or member state=2022-06-22\|Application number in the designated or member state=2022EP-0829238\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP4256520\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2023-10-11\|Publication number in the designated or member state=EP4256520\|Event publication date=2023-02-08\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2023-07-16\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2023-07-03\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2025-12-10\|Event code=WO/WWG\|Event indicator=Pos\|Event group=Event indicating In Force\|Wipo information: grant in national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR HK40095252\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=HK Corresponding appl: HK62023083672\|Application date in the designated or member state=2023-12-05\|Application number in the designated or member state=2023HK-6083672\|Corresponding cc:\|Designated or member state=HK Corresponding pat: HK40095252\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2024-01-26\|Publication number in the designated or member state=HK40095252\|(BR112023023226)\|LEGAL DETAILS FOR BR112023023226\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2022-06-22\|Event code=BR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=BR BR112023023226\|Application date=2022-06-22\|Standardized application number=2023BR-0023226\|Event publication date=2023-11-14\|Event code=BR/A0\|Event indicator=Pos\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=BR\|Publication number=BR112023023226\|Publication stage code=A0\|Publication date=2023-11-14\|Standardized publication number=BR112023023226\|Event publication date=2024-01-30\|Event code=BR/A2\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention / pipeline patent published without search report\|Publication country=BR\|Publication number=BR112023023226\|Publication stage code=A2\|Publication date=2024-01-30\|Standardized publication number=BR112023023226\|Event publication date=2025-09-30\|Event code=BR/B07A\|Event group=Examination events\|Technical examination (opinion): publication of technical examination (opinion)\|Ciencia de parecer: conhecimento de parecer tecnico [codigo 7.1 rpi]\|Event publication date=2025-12-16\|Event code=BR/B09A\|Event group=Event indicating In Force Administrative notifications\|Decision: granting\|Decisao: deferimento [codigo 9.1 rpi]\|Event publication date=2026-01-13\|Event code=BR/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent / Granted pipeline patent\|Publication country=BR\|Publication number=BR112023023226\|Publication stage code=B1\|Publication date=2026-01-13\|Standardized publication number=BR112023023226\|Event publication date=2026-01-13\|Event code=BR/B16A\|Event indicator=Pos\|Event group=Event indicating In Force Administrative notifications\|Patent or certificate of addition of invention granted\|Concessao de patente ou certificado de adicao de invencao [codigo 16.1 rpi]\|Prazo de validade: 20 (VINTE) ANOS CONTADOS A PARTIR DE 22/06/2022, OBSERVADAS AS CONDICOES LEGAIS\|(AU2022299180)\|LEGAL DETAILS FOR AU2022299180\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-06-22\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2022299180\|Application date=2022-06-22\|Standardized application number=2022AU-0299180\|Event publication date=2023-07-13\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2022299180\|Publication stage code=A1\|Publication date=2023-07-13\|Standardized publication number=AU2022299180\|Event publication date=2024-10-24\|Event code=AU/A9\|Event indicator=Pos\|Event group=Examination events\|Corrected complete document\|Publication country=AU\|Publication number=AU2022299180\|Publication stage code=A9\|Publication date=2024-10-24\|Standardized publication number=AU2022299180\|Event publication date=2024-10-24\|Event code=AU/SREP\|Event group=Administrative notifications\|Specification republished\|(HK40095252)\|LEGAL DETAILS FOR HK40095252\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-12-05\|Event code=HK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=HK HK62023083672\|Application date=2023-12-05\|Standardized application number=2023HK-6083672\|Event publication date=2024-01-26\|Event code=HK/A\|Event indicator=Pos\|Event group=Examination events\|Standard patent (R) application\|Publication country=HK\|Publication number=HK40095252\|Publication stage code=A\|Publication date=2024-01-26\|Standardized publication number=HK40095252\|(HK40094979)\|LEGAL DETAILS FOR HK40094979\|Actual or expected expiration date=2043-12-05\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-12-05\|Event code=HK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=HK HK42023083673\|Application date=2023-12-05\|Standardized application number=2023HK-4083673\|Event publication date=2024-01-26\|Event code=HK/A\|Event indicator=Pos\|Event group=Examination events\|Standard patent (R) application\|Publication country=HK\|Publication number=HK40094979\|Publication stage code=A\|Publication date=2024-01-26\|Standardized publication number=HK40094979\|(CA3207124)\|LEGAL DETAILS FOR CA3207124\|Actual or expected expiration date=2042-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-06-22\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA3207124\|Application date=2022-06-22\|Standardized application number=2022CA-3207124\|Event publication date=2022-12-29\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA3207124\|Publication stage code=A1\|Publication date=2022-12-29\|Standardized publication number=CA3207124\|Event publication date=2025-06-13\|Event code=CA/MFA\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|MAINTENANCE FEE FOR APPLICATION PAID\|Annual fees payment date=2025-06-13\|Year of payment of annual fees=3\|Fee description text: MF (APPLICATION, 3RD ANNIV.) - STANDARD\|Event publication date=2025-06-13\|Event code=CA/U00\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FEE PAID\|ST27 STATUS EVENT CODE: A-1-1-U10-U00-U101 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE REQUEST RECEIVED\|Effective date of the event=2025-06-13\|Event publication date=2025-06-13\|Event code=CA/U11\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FULL RENEWAL OR MAINTENANCE FEE PAID\|ST27 STATUS EVENT CODE: A-1-1-U10-U11-U102 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE FEE PAYMENT PAID IN FULL\|Effective date of the event=2025-06-13\|Event publication date=2026-01-13\|Event code=CA/P22\|Event group=Classification modifications Corrections\|CLASSIFICATION MODIFIED\|ST27 STATUS EVENT CODE: A-1-1-P10-P22-P110 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: CLASSIFICATION MODIFIED\|Effective date of the event=2026-01-13	(EP4256520)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4256520)\|UP Participating States: EE, DE, BE, FI, PT, BG, DK, MT, LT, LU, LV, IT, FR, SE, AT, SI, RO, NL\|(EP4276752)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4276752)\|Extension States: ME, BA\|(EP4276752)\|Validation States: MA, MD, TN, KH\|(WO2022/271842)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2022/271842)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2022/271842)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2022/271842)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2022/271842)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP4256520)\|EP; AT; BE; BG; CH; DE; DK; EE; EP; FI; FR; GB; HK; IE; IT; LT; LU; LV; MT; NL; PT; RO; SE; SI\|(EP4276752)\|EP; EP; HK\|(US12422425)\|US\|(US11921098)\|US\|(US11644454)\|US\|(US20260016458)\|US\|(WO2022/271842)\|AU; BR; CA; EP; HK\|(BR112023023226)\|BR\|(AU2022299180)\|AU\|(HK40095252)\|HK\|(HK40094979)\|HK\|(CA3207124)\|CA	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcNZZqLpDi64+bxtUVS6odf4JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP0000000011088080&ekey=1957&xpn=EP4256520&kind=C0	https://register.epo.org/application?number=EP22829238	https://permalink.orbit.com/RenderStaticFirstPage?XPN=V1%252BTlYp%252BvobVNtz%252BuaPnF3fDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(US20260016458)\|US\|(US12422425)\|US\|(US20240264139)\|US\|(HK40094979)\|US\|(US11921098)\|US\|(US20230273174)\|US\|(WO2022/271842)\|US\|(US11644454)\|US\|(US20220404329)\|US	(US20260016458)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US\|(US12422425)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US , ATYP=US Company\|(US20240264139)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US\|(HK40094979)\|NAME=Eion Corp 82 Spruce St., Princeton, New Jersey 08542 , COUNTRY=US\|(US11921098)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US , ATYP=US Company\|(US20230273174)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US\|(WO2022/271842)\|NAME=EION CORP. 82 Spruce St. Princeton, New Jersey 08542 , COUNTRY=US\|(US11644454)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US , ATYP=US Company\|(US20220404329)\|NAME=Eion Corp. , CITY=Princeton , STATE=NJ , COUNTRY=US	(EP4256520)\|IT\|(EP4256520)\|IT\|(EP4276752)\|IT\|(EP4276752)\|IT\|\|\|\|(WO2022/271842)\|US\|(AU2022299180)\|NZ\|(AU2022299180)\|NZ\|(HK40095252)\|HK\|(HK40094979)\|HK\|(CA3207124)\|CA	(EP4256520)\|NAME=Dragotti & Associati S.P.A. Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101869514\|(EP4256520)\|NAME=Pistolesi, Roberto;Dragotti & Associati Srl Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101195246\|(EP4276752)\|NAME=Dragotti & Associati S.R.L. Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101869514\|(EP4276752)\|NAME=Pistolesi, Roberto;Dragotti & Associati Srl Via Nino Bixio, 7 , CITY=20129 Milano , COUNTRY=IT , REG=101195246\|(US12422425)\|NAME=Frost Brown Todd LLP NAME=VanDrake, III Vance V. NAME=Johnson Alexander J.\|(US11921098)\|NAME=Frost Brown Todd LLP NAME=VanDrake, III Vance V. NAME=Johnson Alexander J.\|(US11644454)\|NAME=Ulmer & Berne LLP NAME=Van Drake, III Vance V. NAME=Johnson Alexander J.\|(WO2022/271842)\|NAME=FALK, Daniel T. et al. 1660 W. 2nd Street Suite 1100 Cleveland, Ohio 44113 , POSTCODE=44113 , COUNTRY=US\|(AU2022299180)\|NAME=AJ Pietras IP Limited Level 2, Bloomfield House 46/50 Bloomfield Terrace , CITY=Lower Hutt , STATE=Wellington , POSTCODE=5010 , COUNTRY=NZ\|(AU2022299180)\|NAME=AJ Pietras IP Limited Level 1, 29 Kings Crescent , CITY=Lower Hutt , STATE=Wellington , POSTCODE=5010 , COUNTRY=NZ\|(HK40095252)\|NAME=HNC INNOVATION LIMITED , COUNTRY=HK\|(HK40094979)\|NAME=HNC INNOVATION LIMITED , COUNTRY=HK\|(CA3207124)\|NAME=BURNET, DUCKWORTH & PALMER LLP , COUNTRY=CA	\|(EP4256520)\|US; US; US\|\|(EP4256520)\|US; US; US\|(EP4276752)\|US; US; US\|(EP4276752)\|US; US; US\|(US12422425)\|US; US; US\|(US20240264139)\|US; US; US\|(US11921098)\|US; US; US\|(US20230273174)\|US; US; US\|(US11644454)\|US; US; US\|(US20220404329)\|US; US; US\|(US20260016458)\|US; US; US\|(WO2022/271842)\|US; US; US\|\|\|\|\|\|\|(CA3207124)\|US; US; US	(EP4256520)\|NAME=WOLF, Adam\|NAME=CHANG, Elliot Suk-Hyun\|NAME=TANK, Alan Robert\|(EP4256520)\|NAME=WOLF, Adam, CITY=Princeton, New Jersey 08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun, CITY=Berkeley, California 94703, COUNTRY=US \|NAME=TANK, Alan Robert, CITY=Bethesda, Maryland 20816, COUNTRY=US\|(EP4256520)\|NAME=WOLF, Adam\|NAME=CHANG, Elliot Suk-Hyun\|NAME=TANK, Alan Robert\|(EP4256520)\|NAME=WOLF, Adam, CITY=Princeton, New Jersey 08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun, CITY=Berkeley, California 94703, COUNTRY=US \|NAME=TANK, Alan Robert, CITY=Bethesda, Maryland 20816, COUNTRY=US\|(EP4276752)\|NAME=WOLF, Adam, CITY=Princeton, 08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun, CITY=Foster City, 94404, COUNTRY=US \|NAME=TANK, Alan Robert, CITY=Bethesda, 20816, COUNTRY=US\|(EP4276752)\|NAME=WOLF, Adam, CITY=Princeton, 08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun, CITY=Foster City, 94404, COUNTRY=US \|NAME=TANK, Alan Robert, CITY=Bethesda, 20816, COUNTRY=US\|(US12422425)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US20240264139)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US11921098)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US20230273174)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US11644454)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US20220404329)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(US20260016458)\|NAME=Wolf Adam, CITY=Princeton, STATE=NJ , COUNTRY=US \|NAME=Chang Elliot Suk-Hyun, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Tank Alan Robert, CITY=Bethesda, STATE=MD , COUNTRY=US\|(WO2022/271842)\|NAME=WOLF, Adam 82 Spruce St. Princeton, New Jersey 08542, POSTCODE=08542, COUNTRY=US \|NAME=CHANG, Elliot Suk-Hyun 1905 Grant Street Berkeley, California 94703, POSTCODE=94703, COUNTRY=US \|NAME=TANK, Alan Robert 5324 Portsmouth Road Bethesda, Maryland 20816, POSTCODE=20816, COUNTRY=US\|(BR112023023226)\|NAME=WOLF ADAM\|NAME=CHANG ELLIOT SUK-HYUN\|NAME=TANK ALAN ROBERT\|(BR112023023226)\|NAME=WOLF ADAM\|NAME=CHANG ELLIOT SUK-HYUN\|NAME=TANK ALAN ROBERT\|(AU2022299180)\|NAME=WOLF, Adam\|NAME=CHANG, Elliot Suk-Hyun\|NAME=TANK, Alan Robert\|(AU2022299180)\|NAME=WOLF, Adam\|NAME=CHANG, Elliot Suk-Hyun\|NAME=TANK, Alan Robert\|(HK40095252)\|NAME=WOLF Adam\|NAME=CHANG Elliot Suk-Hyun\|NAME=TANK Alan Robert\|(HK40094979)\|NAME=WOLF Adam\|NAME=CHANG Elliot Suk-Hyun\|NAME=TANK Alan Robert\|(CA3207124)\|NAME=WOLF, ADAM, COUNTRY=US \|NAME=CHANG, ELLIOT SUK-HYUN, COUNTRY=US \|NAME=TANK, ALAN ROBERT, COUNTRY=US	(US20260016458)\|4\|(US12422425)\|4\|(US11921098)\|4\|(WO2022/271842)\|4\|\|(CA3207124)\|4\|(US11644454)\|4	9	12			(EP4256520)\|WO2022/271842\|(EP4276752)\|WO2022/271842\|(BR112023023226)\|WO2022/271842\|(AU2022299180)\|WO2022/271842\|(HK40095252)\|WO2022/271842\|(CA3207124)\|WO2022/271842	(EP4276752)\|EP22829238	(EP4256520)\|Gazette date: GAZDATE=2025-12-10\|\|(EP4256520)\|Number of Claims: NCL=8\|\|Primary examiner: Poole, Robert\|\|(EP4276752)\|Number of Claims: NCL=10\|22.09.2023 as a divisional application to the application mentioned under INID code 62.\|Primary examiner: Poole, Robert\|\|(US12422425)\|Number of Claims: NCL=10\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=0\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US20240264139)\|Number of Claims: NCL=10\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US11921098)\|Number of Claims: NCL=10\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US20230273174)\|Number of Claims: NCL=10\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US11644454)\|Number of Claims: NCL=11\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US20220404329)\|Number of Claims: NCL=21\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1,12\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: Nguyen Kiet T\|Art Unit.: ART =2881\|\|(US20260016458)\|Number of Claims: NCL=11\|Number of Drawings: NDR=3\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|\|(WO2022/271842)\|Number of Claims: NCL=21\|Extended kind: EXTK=x\|\|(BR112023023226)\|Prazo de Validade: 20 (vinte) anos contados a partir de 22/06/2022, observadas as condições legais\|\|(CA3207124)\|Number of Claims: NCL=21\|	(EP4276752)\|Division of: EP22829238 FDD=2022-06-22 [2022EP-0829238]\|(US12422425)\|Continuation of: US18/128,583 FDD=2023-03-30 [2023US-18128583]\|Division of: US17/846,838 FDD=2022-06-22 [2022US-17846838]\|Continuation of: US11921098 \|Division of: US11644454 2023-04-19 [US11644454]\|Provisional Appl: US63/322,672 FDD=2022-03-23 [2022US-63322672]\|Provisional Appl: US63/289,395 FDD=2021-12-14 [2021US-63289395]\|Provisional Appl: US63/213,398 FDD=2021-06-22 [2021US-63213398]\|Previous publication: US20240264139 A1 2024-08-08 [US20240264139]\|(US11921098)\|Division of: US17/846,838 FDD=2022-06-22 [2022US-17846838]\|Division of: US11644454 \|Provisional Appl: US63/322,672 FDD=2022-03-23 [2022US-63322672]\|Provisional Appl: US63/289,395 FDD=2021-12-14 [2021US-63289395]\|Provisional Appl: US63/213,398 FDD=2021-06-22 [2021US-63213398]\|Previous publication: US20230273174 A1 2023-08-31 [US20230273174]\|(US11644454)\|Provisional Appl: US63/322,672 FDD=2022-03-23 [2022US-63322672]\|Provisional Appl: US63/289,395 FDD=2021-12-14 [2021US-63289395]\|Provisional Appl: US63/213,398 FDD=2021-06-22 [2021US-63213398]\|Previous publication: US20220404329 A1 2022-12-22 [US20220404329]\|(US20260016458)\|Continuation of: US18/435,492 FDD=2024-02-07 [2024US-18435492]\|Continuation of: US18/128,583 FDD=2023-03-30 [2023US-18128583]\|Division of: US17/846,838 FDD=2022-06-22 [2022US-17846838]\|Continuation of: US12422425 \|Continuation of: US11921098 \|Division of: US11644454 \|Provisional Appl: US63/213,398 FDD=2021-06-22 [2021US-63213398]\|Provisional Appl: US63/289,395 FDD=2021-12-14 [2021US-63289395]\|Provisional Appl: US63/322,672 FDD=2022-03-23 [2022US-63322672]\|(CA3207124)\|Division of: CA3207124 FDD=2022-06-22 [2022CA-3207124]	(EP4256520)\|ENGLISH (ENG)	(US20260016458)\|Patent\|(BR112023023226)\|Patent\|(EP4256520)\|Patent\|(EP4256520)\|Patent\|(US12422425)\|Patent\|(EP4256520)\|Patent\|(AU2022299180)\|Patent\|(US20240264139)\|Patent\|(EP4276752)\|Patent\|(US11921098)\|Patent\|(BR112023023226)\|Patent\|(HK40094979)\|Patent\|(HK40095252)\|Patent\|(EP4276752)\|Patent\|(BR112023023226)\|Patent\|(EP4256520)\|Patent\|(US20230273174)\|Patent\|(AU2022299180)\|Patent\|(US11644454)\|Patent\|(CA3207124)\|Patent\|(WO2022271842)\|Patent\|(US20220404329)\|Patent	Titre: (EP4256520)\|Verification methods and agronomic enhancements for carbon removal based on enhanced rock weathering Résumé: (EP4256520)\|The present disclosure relates to methods of verifying enhanced rock weathering using immobile trace elements found within a mineral amendment. Further disclosed are mineral amendments that enable enhanced rock weathering.	3	Abstract	gpt-4o-mini	yes	The article discusses methods for verifying enhanced rock weathering and mentions mineral amendments that facilitate this process, which aligns with the goal of carbon sequestration through accelerated weathering.
3	US63/669,351P\|US19/264,502	US19/264,502	US20260017435	117356463	US20260017435 A1 2026-01-15 [US20260017435]	2024-07-10\|2025-07-09	2025-07-09	2026-01-15		(US20260017435)\|2045-07-09	(US20260017435)\|Technologies for modeling carbon dioxide removal	(US20260017435)\|Technologies for modeling carbon dioxide removal include a compute device with circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may also be configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Further, the circuitry may be configured to present a visual representation of the at least one prediction in a user interface. Other embodiments are also described and claimed.	UNIVERSITY INDIANA TRUSTEES	(US20260017435)\|THE TRUSTEES OF INDIANA UNIVERSITY ([US])	ZHU CHEN	(US20260017435)\|Zhu Chen		(US20260017435)\|A modeling forecast is useful at every stage of a project: conceptualization, contract negotiation, application, and post-project monitoring.\|There exists a plurality of advantages of the present disclosure arising from the various features of the apparatus, systems, and methods described herein.\|Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.\|	(US20260017435)\|1. A compute device comprising: circuitry configured to: obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and present a visual representation of the at least one prediction in a user interface.\|14. A method comprising: obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and presenting, by the compute device, a visual representation of the at least one prediction in a user interface.\|19. One or more machine-readable storage media comprising a plurality of instructions stored thereon that, in response to being executed, cause a compute device to: obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and present a visual representation of the at least one prediction in a user interface.\|	(US20260017435)\|Further, the system 100 provides provenance for the execution of tools, clonability, and reusability and integrates with national open cyberinfrastructure and public clouds for workflow execution.\|In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. The system 100, in operation, provides innovative and independent geochemical models and modeling forecasts, filling a current gap in monitoring, reporting, and verification (MRV).\|The present application discloses one or more of the features recited in the appended claims and/or the following features which, alone or in any combination, may comprise patentable subject matter:According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering.\|	(US20260017435)\|ENHANCED ROCK(100,28)\|MODELING CARBON DIOXIDE REMOVAL(100,6)\|IRON COPRECIPITATION(94,11)\|FORECAST MODEL(65,1)\|FORECASTING MODEL(65,1)\|VISUAL REPRESENTATION(59,20)\|WORKFLOW EXECUTION(57,1)\|NATIONAL OPEN CYBER INFRASTRUCTURE(56,1)\|SATISFYING CONCERN(54,1)\|PARAMETER DATA(53,57)\|OPEN CYBER INFRASTRUCTURE(47,1)\|GEOCHEMICAL MODEL(41,3)\|CONCEPTUALIZATION(36,1)\|CARBON DIOXIDE(33,77)\|CLONABILITY(32,1)\|REUSABILITY(32,1)\|NEGOTIATION(31,1)\|PROVENANCE(31,1)\|POST PROJECT MONITORING(30,1)\|ENHANCE REMOVAL(28,1)\|VERIFICATION(28,1)\|REPORTING(27,1)\|SCIENCE GATEWAY(27,1)\|COMPUTE DEVICE(26,45)\|BASALT WEATHERING(25,6)\|PUBLIC CLOUD(25,1)\|MODELING COMPUTE DEVICE(24,92)\|UNIDIRECTIONAL RATE(24,6)\|SOILS(23,1)\|GROUND(22,45)\|CARBON DIOXIDE REMOVAL(22,12)\|GATEWAY(21,15)\|TOXIC METAL(20,24)\|PREDICTION VISUAL REPRESENTATION(19,5)\|USER INTERFACE(16,21)\|LIBRARY(15,7)\|IRREVERSIBLE REACTION(15,6)\|MACHINE LEARNING MODEL(15,4)\|STORAGE MEDIA(14,3)\|HECTARE(13,12)\|BASALT TON(12,2)\|TOXIC METAL RELEASE(12,2)\|NEAR EQUILIBRIUM RATE(11,5)\|DATABASE(10,15)\|LOCATION DISTANCE(10,4)\|BLIND PORE(10,3)\|INTERACTIVE GRAPH(10,3)\|SOIL PARAMETER(10,3)\|NICKEL VISUAL REPRESENTATION(10,2)\|ACOUSTIC TOUCHSCREEN SENSOR(10,1)\|ENHANCED ROCK WEATHERING BATCH(10,1)\|SANDSTONE AQUIFER(10,1)\|SEMIEMPIRICAL SCALING FACTOR(10,1)\|WORLDWIDE INTEROPERABILITY(10,1)\|SUBSYSTEM(9,7)\|COMMUNICATION CIRCUITRY(9,6)\|OBTAINING PARAMETER DATA(9,6)\|PREDICTED(9,6)\|PROBABILITY(8,5)\|BASALT DENSITY(8,3)\|TOPSOIL LAYER(8,3)\|CYBER INFRASTRUCTURE(8,1)\|GEOCHEMICAL EXPERT(8,1)\|INFRARED TOUCHSCREEN SENSOR(8,1)\|LEVERAGE EXPERTIZE(8,1)\|MINE TAILING(8,1)\|RENDING ENGINE(8,1)\|WEB INTERFACE(7,5)\|BULK SOIL DENSITY(7,4)\|APPLICABLE REGULATION(7,2)\|NONVOLATILE MEMORY(7,2)\|SOIL DEPTH(7,2)\|BASALT MINERAL MAKEUP(7,1)\|GRAPHICAL PRESENTATION(7,1)\|INTERPRETABLE MODEL(7,1)\|MULTICHIP PACKAGE(7,1)\|NUMB INDICATIVE(7,1)\|PORTABLE NETWORK GRAPHICS(7,1)\|PURCHASER CORPORATION(7,1)\|RECONFIGURABLE HARDWARE(7,1)\|SIMILARITY SCORE(7,1)\|SIMILARITY DETERMINATION(6,3)\|STAKEHOLDER(6,3)\|AUTOMATIC DOCUMENTATION(6,1)\|BASALT MASS(6,1)\|BIODIVERSITY LOSS(6,1)\|CAPACITIVE TOUCHSCREEN SENSOR(6,1)\|CLUSTERING ANALYSIS(6,1)\|ENCODED INSTRUCTION(6,1)\|GROWING CONCERN(6,1)\|IRRIGATION WATER REGULATION(6,1)\|OXY HYDROXIDE(6,1)\|PARAMETER DATA REFORMATTING(6,1)\|RESISTIVE TOUCHSCREEN SENSOR(6,1)\|SIMULATION CONFIDENCE INTERVAL(6,1)\|SOIL REGULATION(6,1)\|SPECIALIZED HARDWARE(6,1)\|VISUAL PRESENTATION(6,1)\|CADMIUM(5,4)\|CHROMIUM(5,4)\|AIR CALCULATION(5,2)\|CUBIC CENTIMETER(5,2)\|DRINKING WATER REGULATION(5,2)\|GEOCHEMICAL MODELING(5,2)\|GEOGRAPHIC COORDINATE(5,2)\|NONEXPERT(5,2)\|PHREEQC(5,2)\|CARBON CAPTURE PREDICTION(5,1)\|CARBON CAPTURE SIMULATION(5,1)\|CARBON CREDIT MARKET(5,1)\|COAXIAL NETWORK(5,1)\|COMPLEX INTERACTION(5,1)\|CONTROLLER CHIP(5,1)\|CREDIT ABILITY(5,1)\|DIGITAL VERSION(5,1)\|ENHANCE CAPTURE(5,1)\|FEED STOCK(5,1)\|FILE FORMAT(5,1)\|FIRMWARE CODE(5,1)\|HARDWARE CIRCUITRY(5,1)\|MICROWAVE ACCESS(5,1)\|OPTICAL IMAGING TOUCHSCREEN SENSOR(5,1)\|PREDICATION(5,1)\|SIMULATION PRODUCT(5,1)\|WEB MODEL INTERFACE(5,1)\|GRAM(4,3)\|USER INPUT(4,3)\|PREDICTION ACCURACY(4,2)\|ADJUSTED PARAMETER(3,1)\|ARCHIVE(3,1)\|AUTHORIZATION(3,1)\|BLUETOOTH(3,1)\|BUS LINK(3,1)\|CARBON DIOXIDE TRAP ENERGY(3,1)\|CERTIFICATION(3,1)\|CHIPSET(3,1)\|COPRECIPITATION(3,1)\|COSINE SIMILARITY(3,1)\|DAUGHTER CARD(3,1)\|DISRUPTION(3,1)\|DROUGHT(3,1)\|ENCODING(3,1)\|ENSEMBLE(3,1)\|EXECUTABLE(3,1)\|FACILITY(3,1)\|FIBER NETWORK(3,1)\|FIND PATTERN(3,1)\|FLOODING(3,1)\|GEOLOGICAL SURVEY(3,1)\|GESTURE(3,1)\|GIGATON LEVEL(3,1)\|GREENHOUSE GAS ATMOSPHERE(3,1)\|HYPERTEXT MARKUP LANGUAGE(3,1)\|IDENTIFICATION(3,1)\|INCLUSION(3,1)\|INDUSTRY STANDARD AUTHENTICATION(3,1)\|INTEGRATED SENSOR HUB(3,1)\|KEYBOARD(3,1)\|LYSIMETER EXPERIMENTAL DATA(3,1)\|MAKE MODELING(3,1)\|	(US20260017435)\|1. A compute device comprising:\| circuitry configured to:\| obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering;\| produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| present a visual representation of the at least one prediction in a user interface.\|2. The compute device of claim 1, wherein to produce, using one or more models from a library of models, at least one prediction comprises to simulate basalt weathering as irreversible reactions with unidirectional rates.\|3. The compute device of claim 1, wherein to produce, using one or more models from a library of models, at least one prediction comprises to utilize one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates.\|4. The compute device of claim 1, wherein to produce, using one or more models from a library of models, at least one prediction comprises to utilize one or more models that simulate co-precipitation of iron with toxic metals.\|5. The compute device of claim 1, wherein to obtain parameter data comprises to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured.\|6. The compute device of claim 1, wherein to obtain parameter data comprises to obtain the parameter data as a function of an identification of the location where the carbon dioxide is to be captured.\|7. The compute device of claim 1, wherein the circuitry is further configured to calculate, as a function of the obtained parameter data, additional parameter data for use by the one or more models.\|8. The compute device of claim 1, wherein to produce at least one prediction comprises to select one or more models as a function of the obtained parameter data.\|9. The compute device of claim 1, wherein to produce at least one prediction comprises to select one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library.\|10. The compute device of claim 1, wherein to produce at least one prediction comprises to utilize one or more machine learning models.\|11. The compute device of claim 1, wherein to produce at least one prediction comprises to produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period.\|12. The compute device of claim 1, wherein to produce at least one prediction comprises to produce one or more predictions indicative of tons of carbon dioxide captured per unit of area.\|13. The compute device of claim 1, wherein to produce at least one prediction comprises to produce at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured.\|14. A method comprising:\| obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering;\| producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| presenting, by the compute device, a visual representation of the at least one prediction in a user interface.\|15. The method of claim 14, wherein producing, using one or more models from a library of models, at least one prediction comprises simulating basalt weathering as irreversible reactions with unidirectional rates.\|16. The method of claim 14, wherein producing, using one or more models from a library of models, at least one prediction comprises utilizing one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates.\|17. The method of claim 14, wherein producing, using one or more models from a library of models, at least one prediction comprises utilizing one or more models that simulate co-precipitation of iron with toxic metals.\|18. The method of claim 14, wherein obtaining parameter data comprises obtaining data indicative of properties of soil in a location where the carbon dioxide is to be captured.\|19. One or more machine-readable storage media comprising a plurality of instructions stored thereon that, in response to being executed, cause a compute device to:\| obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering;\| produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| present a visual representation of the at least one prediction in a user interface.\|20. The one or more machine-readable storage media of claim 19, wherein to obtain parameter data comprises to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured.	(US20260017435)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/669,351 filed on Jul. 10, 2024, the disclosure of which is expressly incorporated herein.\|(US20260017435)\|BACKGROUND\|[0002] Climate change is a growing concern across the world as atmospheric greenhouse gases such as carbon dioxide trap energy radiated from the sun. While a direct result of increases in greenhouse gases is increased temperatures on Earth, knock on effects include droughts, flooding, loss of biodiversity, and disruptions in energy and transportation systems across the world. Through interactions between water and rock (e.g., in soil), carbon dioxide can be captured (e.g., removed) from the atmosphere and correspondingly lessen the effects of climate change. However, given the multitude of factors that influence the complex interactions between water and rock, it is not feasible in conventional computerized systems to reliably determine the amount of carbon dioxide that will be removed in a given location, under a given set of conditions, or to predict side effects of any efforts to enhance the capture of carbon dioxide in the soil. Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.\|SUMMARY\|[0003] The present application discloses one or more of the features recited in the appended claims and/or the following features which, alone or in any combination, may comprise patentable subject matter:\|[0004] According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may be further configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. Producing a prediction may include simulating co-precipitation of iron with one or more toxic metals. The circuitry may be further configured to present a visual representation of the at least one prediction in a user interface.\|[0005] In some embodiments, the circuitry may be configured such that using one or more models from a library of models to produce at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. The circuitry may also be configured to utilize one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, the circuitry may be configured to utilize one or more models that simulate co-precipitation of iron with toxic metals. The circuitry may be configured to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that obtaining data indicative of properties of soil includes obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and basalt mineral composition.\|[0006] The circuitry may be configured such that obtaining parameter data includes obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured to obtain parameter data as a function of an identification of the location where the carbon dioxide is to be captured by reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. The circuitry may be configured to obtain parameter data through user input into corresponding fields of a user interface. In some embodiments, the circuitry may be further configured to calculate, as a function of the obtained parameter data, additional parameter data for use by the one or more models. The circuitry may be configured such that calculating additional parameter data involves calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.\|[0007] In some embodiments, calculating additional parameter data further includes utilizing a database of specific surface areas for each of a set of minerals. The compute device, in some embodiments, may include circuitry configured to select one or more models as a function of the obtained parameter data. In some embodiments, the circuitry may be configured such that to select one or more models as a function of the obtained parameter data includes selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, the circuitry is configured such that producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. In some embodiments, the circuitry is configured such that producing at least one prediction includes reformatting the parameter data for use by the one or more models.\|[0008] The circuitry may be configured such that producing at least one prediction includes utilizing one or more machine learning models. Additionally or alternatively, the circuitry may be configured utilize an ensemble of models to produce the at least one prediction. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period. The circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, the circuitry may be configured such that to produce at least one prediction involves producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured per hectare.\|[0009] The circuitry may be configured to produce at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, the circuitry is configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time. The circuitry may be configured such that to produce the at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions.\|[0010] In some embodiments, the circuitry may be configured such that to produce at least one prediction involves determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. The compute device, in some embodiments, may have circuitry configured such that to produce at least one prediction involves determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. In some embodiments, the circuitry may be further configured to determine, from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, the circuitry is configured such that to present a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.\|[0011] According to another aspect of the present disclosure, a method includes obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The method may further include producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. In doing so, the method may include simulating co-precipitation of iron with one or more toxic metals. The method may further include presenting, by the compute device, a visual representation of the at least one prediction in a user interface.\|[0012] In some embodiments, producing, using one or more models from a library of models, at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. Producing, using one or more models from a library of models, at least one prediction may, in some embodiments, include utilizing one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, producing, using one or more models from a library of models, at least one prediction may include utilizing one or more models that simulate co-precipitation of iron with toxic metals. Obtaining parameter data may, in some embodiments, include obtaining data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, obtaining data indicative of properties of soil may include obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and a basalt mineral composition.\|[0013] Obtaining parameter data may include obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. Obtaining parameter data as a function of an identification of the location where the carbon dioxide is to be captured may include reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. Obtaining parameter data may include obtaining parameter data through user input into corresponding fields of a user interface. The method may also include calculating, by the compute device and as a function of the obtained parameter data, additional parameter data for use by the one or more models. Calculating additional parameter data may include calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.\|[0014] In some embodiments, calculating additional parameter data may additionally include utilizing a database of specific surface areas for each of a set of minerals. Producing at least one prediction may include selecting one or more models as a function of the obtained parameter data. Selecting one or more models as a function of the obtained parameter data may involve selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. Producing at least one prediction may include reformatting the parameter data for use by the one or more models. In some embodiments, producing at least one prediction involves utilizing one or more machine learning models. Producing at least one prediction may, in some embodiments, include utilizing an ensemble of models to produce the at least one prediction. Producing at least one prediction may include producing one or more predictions indicative of tons of carbon dioxide captured over a predefined time period.\|[0015] Producing one or more predictions may include producing one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, producing at least one prediction includes producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. Producing one or more predictions may, in some embodiments, include producing one or more predictions indicative of tons of carbon dioxide captured per hectare. In some embodiments, producing at least one prediction includes producing at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. Producing at least one prediction indicative of toxic metal concentrations in water may, in some embodiments, involve producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, producing at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time.\|[0016] Producing the at least one prediction indicative of toxic metal concentrations in water may involve producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, producing the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions. Producing at least one prediction may include determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. In some embodiments, producing at least one prediction includes determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. The method may also include determining, by the compute device and from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, presenting a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.\|[0017] According to another aspect of the present disclosure, one or more machine-readable storage media may include instructions stored thereon that, in response to being executed, cause a compute device to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The instructions may further cause the compute device to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Additionally, the instructions may cause the compute device to present a visual representation of the at least one prediction in a user interface. Further, the instructions may cause the compute device to perform any of the methods described above.\|[0018] Additional features, which alone or in combination with any other feature(s), such as those listed above and/or those listed in the claims, may comprise patentable subject matter and will become apparent to those skilled in the art upon consideration of the following detailed description of various embodiments exemplifying the best mode of carrying out the embodiments as presently perceived.\|(US20260017435)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0019] The concepts described herein are illustrated by way of example and not by way of limitation in the accompanying figures. For simplicity and clarity of illustration, elements illustrated in the figures are not necessarily drawn to scale. Where considered appropriate, reference labels have been repeated among the figures to indicate corresponding or analogous elements. The detailed description particularly refers to the accompanying figures in which:\|[0020] FIG. 1 is a simplified block diagram of at least one embodiment of a system for modeling carbon dioxide removal through enhanced rock weathering;\|[0021] FIG. 2 is a simplified block diagram of at least one embodiment of a compute device of the system of FIG. 1;\|[0022] FIGS. 3-7 are flowcharts of at least one embodiment of a method for modeling carbon dioxide removal through enhanced rock weathering that may be performed by the system of FIG. 1;\|[0023] FIGS. 8 and 9 are user interfaces that may be produced by the system of FIG. 1; and\|[0024] FIG. 10 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating carbon capture as a function of years;\|[0025] FIG. 11 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating a simulation of carbon capture as a function of time;\|[0026] FIG. 12 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating the confidence interval of the simulations over a five year period;\|[0027] FIG. 13 is one embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1; and\|[0028] FIG. 14 is another embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1\|(US20260017435)\|DETAILED DESCRIPTION OF THE DRAWINGS\|[0029] While the concepts of the present disclosure are susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and will be described herein in detail. It should be understood, however, that there is no intent to limit the concepts of the present disclosure to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives consistent with the present disclosure and the appended claims.\|[0030] References in the specification to “one embodiment,” “an embodiment,” “an illustrative embodiment,” etc., indicate that the embodiment described may include a particular feature, structure, or characteristic, but every embodiment may or may not necessarily include that particular feature, structure, or characteristic. Moreover, such phrases are not necessarily referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with an embodiment, it is submitted that it is within the knowledge of one skilled in the art to effect such feature, structure, or characteristic in connection with other embodiments whether or not explicitly described. Additionally, it should be appreciated that items included in a list in the form of “at least one A, B, and C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C). Similarly, items listed in the form of “at least one of A, B, or C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C).\|[0031] The disclosed embodiments may be implemented, in some cases, in hardware, firmware, software, or any combination thereof. The disclosed embodiments may also be implemented as instructions carried by or stored on a transitory or non-transitory machine-readable (e.g., computer-readable) storage medium, which may be read and executed by one or more processors. A machine-readable storage medium may be embodied as any storage device, mechanism, or other physical structure for storing or transmitting information in a form readable by a machine (e.g., a volatile or non-volatile memory, a media disc, or other media device).\|[0032] In the drawings, some structural or method features may be shown in specific arrangements and/or orderings. However, it should be appreciated that such specific arrangements and/or orderings may not be required. Rather, in some embodiments, such features may be arranged in a different manner and/or order than shown in the illustrative figures. Additionally, the inclusion of a structural or method feature in a particular figure is not meant to imply that such feature is required in all embodiments and, in some embodiments, may not be included or may be combined with other features.\|[0033] Referring now to FIG. 1, a system 100 for modeling carbon dioxide removal through enhanced rock weathering includes a set of one or more modeling compute devices 120, a set of source compute devices 140, 142, 144 and a set of target compute devices 150, 152, 154. In operation, the modeling compute devices 120 operate as a gateway 110 through which end users (e.g., scientists, organizations, etc.) of operating target compute devices 150, 152, 154 may view predictions (e.g., forecasts) of how much carbon dioxide will be captured in the soil at a particular location through a process of enhanced rock weathering. In enhanced rock weathering, rock, such as basalt, is added to soil at a location (e.g., one or more hectares of land) in a powdered form to increase the amount of carbon dioxide removed from the atmosphere through interaction between the carbon dioxide, water (e.g., rain), and rock. The composition of the basalt (e.g., mineral composition) as well as properties of the soil itself (e.g., porosity, carbon content, minerals, etc.) influence the amount of carbon dioxide that will be captured and may impact an amount of toxic metals present in the soil and/or water in the location as a result of the chemical processes involved in the capture of the carbon dioxide. As such, given the multitude of factors that can influence the amount of carbon dioxide removal, the modeling compute devices 120 may utilize a library of models 130 (e.g., thousands of models) and a database 132 of properties of minerals that also affect the amount of carbon dioxide that will be captured. The modeling compute devices 120 produce results 134, which may be embodied as data indicative of amount of carbon dioxide that will be captured under the specified conditions. Additionally, the results 134 may indicate the amount of toxic metals that are predicted to be present in the soil and water as a result of the chemical processes. Further, the results may be broken down across multiple years, depths, confidence intervals, or other parameters and may be the product of thousands of simulations using the set of models 130.\|[0034] The source compute devices 140, 142, 144 may provide data indicative of properties of the soil in various locations, properties of basalt (e.g., various feed stocks of basalt), information indicative of a carbon credits market (e.g., an amount of carbon credits associated with an amount of carbon captured or removed from the atmosphere), data indicative of regulations associated with various locations (e.g., drinking water regulations, irrigation water regulations, soil regulations), and/or other data usable by the modeling compute devices 120 in simulating the capture of carbon from the atmosphere through enhanced rock weathering processes.\|[0035] In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. The system 100, in operation, provides innovative and independent geochemical models and modeling forecasts, filling a current gap in monitoring, reporting, and verification (MRV). Further, the system 100 contributes to the trust that is necessary for the scale-up of climate-tech carbon dioxide removal (CDR) industries to the gigaton level. While the system 100, in some embodiments, focuses on enhanced rock weathering, the science and technologies can also be applied to storing carbon dioxide in basalt and sandstone aquifers and mine tailings.\|[0036] A modeling forecast is useful at every stage of a project: conceptualization, contract negotiation, application, and post-project monitoring. The gateway 110, in the illustrative embodiment, is cloud-based, documented, and based on advanced cyberinfrastructure and data sciences that transform how modeling is delivered and how results are archived, analyzed, and presented. The gateway 110, in the illustrative embodiment, provides industry-standard authentication, authorization, and controlled sharing capabilities. Further, the system 100 provides provenance for the execution of tools, clonability, and reusability and integrates with national open cyberinfrastructure and public clouds for workflow execution.\|[0037] In the illustrative embodiment, the gateway 110 may serve four types of clients: a) technical specialists at stakeholders (CDR and purchaser corporations, regulatory agencies, environmental groups) who can search a large library of models 130 to find the likely outcomes for their projects; b) geochemical experts who can develop or tweak their models 130 on the gateway 110, but aided by automatic documentation, archives, and traceability on the gateway; c) stakeholders with no in-house capabilities who wish to outsource the initial development of models 130 and run the models 130 on the gateway 110; d) stakeholders who need independent models as certification. The availability of the gateway 110 may operate to broaden the participation of underrepresented groups and less developed countries, helping achieve the common goal of implementing scalable solutions around the world.\|[0038] Enhanced rock weathering can be generally represented with the equations shown below:\|[0039] Other equations representative of geochemical reactions are set forth in “Environmental Applications of Geochemical Modeling” by Chen Zhu and Greg Anderson, published in 2002, the contents of which are incorporated herein by reference. As discussed herein, characteristics of the soil and basalt in the soil can significantly impact the amount of carbon dioxide that will be captured and the amounts of metals (e.g., toxic metals) that may be introduced into the soil and water through the enhanced rock wreathing process. The models 130, in the illustrative embodiment, account for the characteristics through parameters discussed herein. Further, the models 130 incorporate features that are not present in conventional modeling systems, including the following: a. Near-equilibrium rates (e.g., in systems with relatively low Gibbs energy) are modeled to be one to two orders of magnitude slower than the far-from-equilibrium rates (e.g., in systems with relatively high Gibbs energy), rather than the far-from-equilibrium rate constants used in other models; b. basalt weathering is simulated as irreversible reactions with unidirectional rates (not reversible reactions in other models, which are theoretically wrong); and c. the models 130 include co-precipitation of toxic metals released from enhanced rock weathering with iron oxyhydroxides. Without co-precipitation in the models 130, the forecasts of toxic metal released into soil may incorrectly indicate toxic metal amounts in excess of applicable regulations. The models 130 may be fine-tuned with time, and more components may be added to the model 130.\|[0040] Further, the system 100, in the illustrative embodiment, provides a web-based model interface. Geochemical models are generally inaccessible to non-experts and the number of experts in the world is in short supply. The system 100 leverages expertise and experience of experts and makes modeling and modeling results available to non-experts. The gateway 110, in the illustrative embodiment, utilizes a database (e.g., the database 132) of mineralogical compositions of basalt feed stocks to be applied to croplands, and provides a web tool (e.g., a web based user interface) that allows users to input mineralogical compositions of the specific feed stock. Behind the web interface, the gateway 110 utilizes a database (e.g., the database 132) of different specific surface areas for different minerals. In operation, the gateway 110 may perform automatic input file generation (e.g., reformatting of parameter data into a format usable by the models 130).\|[0041] The web interface and models enable users (e.g., operating the target compute devices 150, 152, 154) to combine different parameters and run different scenarios to view resulting predictions of carbon capture through enhanced rock weathering and side effects thereof. For example, users may compare how much carbon dioxide is captured by applying 100 tons of basalt per hectare versus ten tons of basalt per hectare, and using one feed stock of basalt (e.g., Oregon basalt) versus another feed stock of basalt (e.g., Columbia River basalt). Users may also view the differences in carbon capture given different particle sizes. Further, users may view data that is indicative of toxic metal release into water and soil under varying conditions.\|[0042] In the illustrative embodiment, the gateway 110 may maintain a library of millions of simulations with a wide range of field conditions. The library may be searchable and the gateway 110 may enable users to locate modeling results and graphic presentations that fit their field conditions within minutes, rather than waiting for hours or longer for simulation results. The library may serve as a base for development or improvement of machine learning algorithms to (1) accelerate the simulations; and (2) find patterns, which lead to faster, more accurate, and more interpretable models. The models 130, in the illustrate embodiment, are calibrated geochemical models that bridge the gap between laboratory and field-based estimates of geochemical reactions. In particular, the models 130 may be calibrated with enhanced rock weathering batch scale laboratory experimental data, field data, and lysimeter experimental data. The results 134 may be embodied as databases and input files with adjusted parameters or semi-empirical scaling factors. In effect, the gateway 110 may provide independent, rigorous, models and modeling results that come with trust and creditability.\|[0043] While a relatively small number of compute devices 120, 140, 142, 144, 150, 152, 154 are shown in FIG. 1 for simplicity and clarity, it should be understood that the number of compute devices, in practice, may range in the tens, hundreds, thousands, or more. Likewise, it should be understood that the compute devices 120, 140, 142, 144, 150, 152, 154 may be distributed differently or perform different roles than the configuration shown in FIG. 1. Further, though shown as separate compute devices 120, 140, 142, 144, 150, 152, 154 in some embodiments, the functionality of one or more of the compute devices 120, 140, 142, 144, 150, 152, 154 may be combined into fewer compute devices and/or distributed across more compute devices than those shown in FIG. 1.\|[0044] Referring now to FIG. 2, an illustrative embodiment of a modeling compute device 120 includes a compute engine 210, an input/output (I/O) subsystem 216, communication circuitry 218, and one or more data storage devices 222. In some embodiments, the modeling compute device 120 may include one or more display devices 224 and/or one or more peripheral devices 226 (e.g., a mouse, a physical keyboard, etc.). In some embodiments, one or more of the illustrative components may be incorporated in, or otherwise form a portion of, another component. The compute engine 210 may be embodied as any type of device or collection of devices capable of performing various compute functions described below. In some embodiments, the compute engine 210 may be embodied as a single device such as an integrated circuit, an embedded system, a field-programmable gate array (FPGA), a system-on-a-chip (SOC), or other integrated system or device. Additionally, in the illustrative embodiment, the compute engine 210 includes or is embodied as a processor 212 and a memory 214. The processor 212 may be embodied as any type of processor capable of performing the functions described herein. For example, the processor 212 may be embodied as a single or multi-core processor(s), a microcontroller, or other processor or processing/controlling circuit. In some embodiments, the processor 212 may be embodied as, include, or be coupled to an FPGA, an application specific integrated circuit (ASIC), reconfigurable hardware or hardware circuitry, or other specialized hardware to facilitate performance of the functions described herein.\|[0045] In embodiments, the processor 212 is capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, a set of instructions which when executed by the processor 212 cause the modeling compute device 120 to perform one or more operations described herein. In embodiments, the processor 212 is further capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, one or more signals from external sources, e.g., from the peripheral devices 226 or via the communication circuitry 218 from an external compute device, external source, or external network. As one will appreciate, a signal may contain encoded instructions and/or information. In embodiments, once received, such a signal may first be stored, e.g., in the memory 214 or in the data storage device(s) 222, thereby allowing for a time delay in the receipt by the processor 212 before the processor 212 operates on a received signal. Likewise, the processor 212 may generate one or more output signals, which may be transmitted to an external device, e.g., an external memory or an external compute engine via the communication circuitry 218 or, e.g., to one or more display devices 224. In some embodiments, a signal may be subjected to a time shift in order to delay the signal. For example, a signal may be stored on one or more storage devices 222 to allow for a time shift prior to transmitting the signal to an external device. One will appreciate that the form of a particular signal will be determined by the particular encoding a signal is subject to at any point in its transmission (e.g., a signal stored will have a different encoding than a signal in transit, or, e.g., an analog signal will differ in form from a digital version of the signal prior to an analog-to-digital (A/D) conversion).\|[0046] The main memory 214 may be embodied as any type of volatile (e.g., dynamic random access memory (DRAM), etc.) or non-volatile memory or data storage capable of performing the functions described herein. Volatile memory may be a storage medium that requires power to maintain the state of data stored by the medium. In some embodiments, all or a portion of the main memory 214 may be integrated into the processor 212. In operation, the main memory 214 may store various software and data used during operation such as models, databases, simulation results, applications, libraries, and drivers.\|[0047] The compute engine 210 is communicatively coupled to other components of the modeling compute device 120 via the I/O subsystem 216, which may be embodied as circuitry and/or components to facilitate input/output operations with the compute engine 210 (e.g., with the processor 212 and the main memory 214) and other components of the modeling compute device 120. For example, the I/O subsystem 216 may be embodied as, or otherwise include, memory controller hubs, input/output control hubs, integrated sensor hubs, firmware devices, communication links (e.g., point-to-point links, bus links, wires, cables, light guides, printed circuit board traces, etc.), and/or other components and subsystems to facilitate the input/output operations. In some embodiments, the I/O subsystem 216 may form a portion of a system-on-a-chip (SoC) and be incorporated, along with one or more of the processor 212, the main memory 214, and other components of the modeling compute device 120, into the compute engine 210.\|[0048] The communication circuitry 218 may be embodied as any communication circuit, device, or collection thereof, capable of enabling communications over a network between the modeling compute device 120 and another device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). The communication circuitry 218 may be configured to use any one or more communication technology (e.g., wired or wireless communications) and associated protocols (e.g., Ethernet, Wi-Fi®, WiMAX, Bluetooth®, etc.) to effect such communication.\|[0049] The illustrative communication circuitry 218 includes a network interface controller (NIC) 220. The NIC 220 may be embodied as one or more add-in-boards, daughter cards, network interface cards, controller chips, chipsets, or other devices that may be used by the modeling compute device 120 to connect with another compute device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). In some embodiments, the NIC 220 may be embodied as part of a system-on-a-chip (SoC) that includes one or more processors, or included on a multichip package that also contains one or more processors. In some embodiments, the NIC 220 may include a local processor (not shown) and/or a local memory (not shown) that are both local to the NIC 220. Additionally or alternatively, in such embodiments, the local memory of the NIC 220 may be integrated into one or more components of the modeling compute device 120 at the board level, socket level, chip level, and/or other levels.\|[0050] Each data storage device 222, may be embodied as any type of device configured for short-term or long-term storage of data such as, for example, memory devices and circuits, memory cards, hard disk drives, solid-state drives, or other data storage device. Each data storage device 222 may include a system partition that stores data and firmware code for the data storage device 222 and one or more operating system partitions that store data files and executables for operating systems.\|[0051] Each display device 224 may be embodied as any device or circuitry (e.g., a liquid crystal display (LCD), a light emitting diode (LED) display, a cathode ray tube (CRT) display, etc.) configured to display visual information (e.g., text, graphics, etc.) to a user. In some embodiments, a display device 224 may be embodied as a touch screen (e.g., a screen incorporating resistive touchscreen sensors, capacitive touchscreen sensors, surface acoustic wave (SAW) touchscreen sensors, infrared touchscreen sensors, optical imaging touchscreen sensors, acoustic touchscreen sensors, and/or other type of touchscreen sensors) to detect selections of on-screen user interface elements or gestures from a user.\|[0052] In the illustrative embodiment, the components of the modeling compute device 120 are housed in a single unit. However, in other embodiments, the components may be in separate housings, in separate racks of a data center, and/or spread across multiple data centers or other facilities. The compute devices 140, 142, 144, 150, 152, 154 may have components similar to those described in FIG. 2 with reference to the modeling compute device 120. The description of those components of the modeling compute device 120 is equally applicable to the description of components of the compute devices 140, 142, 144, 150, 152, 154. Further, it should be appreciated that any of the devices 120, 140, 142, 144, 150, 152, 154 may include other components, sub-components, and devices commonly found in a computing device, which are not discussed above in reference to the modeling compute device 120 and not discussed herein for clarity of the description.\|[0053] In the illustrative embodiment, the compute devices 120, 140, 142, 144, 150, 152, 154 are in communication via a network 160, which may be embodied as any type of wired or wireless communication network, including global networks (e.g., the internet), wide area networks (WANs), local area networks (LANs), digital subscriber line (DSL) networks, cable networks (e.g., coaxial networks, fiber networks, etc.), cellular networks (e.g., Global System for Mobile Communications (GSM), Long Term Evolution (LTE), Worldwide Interoperability for Microwave Access (WiMAX), 3G, 4G, 5G, etc.), a radio area network (RAN), or any combination thereof.\|[0054] Referring now to FIG. 3, the system 100 (e.g., a modeling compute device 120 of the gateway 110) may perform a method 300 for modeling carbon dioxide removal through enhanced rock weathering. The method 300, in the illustrative embodiment, begins with block 302 in which the modeling compute device 120 obtains parameter data indicative of parameters for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering (e.g., the application of basalt dust to soil to increase the amount of carbon dioxide captured through the interaction of water (e.g., rain), carbon dioxide, and rock (e.g., the basalt dust)). In doing so, and as indicated in block 304, the modeling compute device 120 obtains data indicative of properties of soil in a location where the carbon dioxide is to be captured (e.g., removed from the atmosphere through enhanced rock weathering). In the illustrative embodiment, the modeling compute device 120 may obtain data indicative of minerals in the soil (e.g., a numeric value, such as a number indicative of a percentage of the soil comprising minerals), as indicated in block 306. As indicated in block 308, the modeling compute device 120 may obtain data indicative of carbon in the soil (e.g., a numeric value indicative of a percentage of the soil comprising carbon).\|[0055] The modeling compute device 120 may additionally obtain data indicative of effective porosity of the soil where the carbon is to be captured, as indicated in block 310. The effective porosity may be expressed, in at least some embodiments, as a numeric value (e.g., a percentage). As indicated in block 312, the modeling compute device 120 may obtain parameter data indicative of total specific surface area. In at least some embodiments, the total specific surface area may be expressed as square meters per gram. The modeling compute device 120 may obtain data indicative of the height of a top soil layer, as indicated in block 314. The height, in the illustrative embodiment, is expressed in meters. Further, the modeling compute device 120 may obtain data indicative of an amount of basalt added to the soil (e.g., tons per hectare), as indicated in block 316. Further, the modeling compute device 120 may obtain data indicative of basalt density, such as in grams per cubic centimeter, as indicated in block 318. Additionally, the modeling compute device 120 may obtain data indicative of bulk soil density, as indicated in block 320. The bulk soil density, in at least some embodiments, may be expressed as grams per cubic centimeter. The modeling compute device 120 may also obtain data indicative of basalt mineral composition, as indicated in block 322. The mineral composition of the basalt may be structured as one or more pairs of values, with each pair including an identifier (e.g., name, abbreviation, etc.) of a mineral and a corresponding percentage (e.g., indicative of a percentage of the basalt feed stock that the mineral constitutes).\|[0056] Still referring to FIG. 3, the modeling compute device 120 may obtain the parameter data as a function of (e.g., based on) an identification of the location where the carbon dioxide is to be captured in the soil, as indicated in block 324. In doing so, the modeling compute device 120 may read parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of properties of soil associated with location identifiers (e.g., plot numbers, geographic coordinates, zip codes, etc.), as indicated in block 326. In some embodiments, the modeling compute device 120 may obtain parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of mineral compositions from each of multiple basalt feed stocks, as indicated in block 328. Additionally or alternatively, the modeling compute device 120 may obtain parameter data through user input into corresponding fields (e.g., text boxes, check boxes, etc.) of a user interface (e.g., a graphical user interface presented by a target compute device 150, 152, 154 based on code (e.g., hypertext markup language (HTML) and/or JavaScript) and images (e.g., portable network graphics (PNG) files, Joint Photographic Experts Group (JPEG) files, or the like) transmitted from the modeling compute device 120 to the target compute device(s) 150, 152, 154 via the network 160, as indicated in block 330. An embodiment of a user interface 800 with which the modeling compute device 120 may obtain parameter data is shown in FIG. 8. The user interface 800 includes a first screen 810 that comprises parameter data about soil properties and a second screen 820 that includes parameter data about basalt mineral makeup. The user interface 800 provides one embodiment that users can use to input parameters related to soil properties and basalt mineral composition, run the models, and calculate how much CO2 can be sequestered.\|[0057] Referring now to FIG. 4, the method 300 continues in block 332 in which the modeling compute device 120 may calculate, as a function of the obtained parameter data, additional parameter data for use by one or more models (e.g., the models 130). In doing so, the modeling compute device 120 may calculate air and blind pores (e.g., a numeric value), as indicated in block 334. The modeling compute device 120 may additionally calculate a volume of soil per hectare, as indicated in block 336. Further, the modeling compute device 120 may calculate a number of volume (e.g., liters) of pore water per unit of area (e.g., hectare), as indicated in block 338. Additionally, the modeling compute device 120 may calculate a mass of basalt per unit of volume of the soil, as indicated in block 340. In addition, the modeling compute device 120 may calculate a concentration of basalt in the soil, as indicated in block 342. Further, the modeling compute device 120 may calculate a total weight percentage, as indicated in block 344. The modeling compute device 120 may also calculate a rock specific surface area, as indicated in block 346. In addition, the modeling compute device 120 may calculate a total surface area, in block 348. In performing the calculations, the modeling compute device 120 may utilize a database (e.g., a database 132) of specific surface areas for each of a set of minerals (e.g., minerals in the soil, in the basalt, etc.), as indicated in block 350. An embodiment of a user interface 900 in which the modeling compute device 120 may display additional parameters calculated as discussed above is shown in FIG. 9. In some embodiments, the user interface 800 includes a third screen 830 that may display additional parameters calculated as discussed above.\|[0058] After obtaining the parameter data, the method 300, in the illustrative embodiment, advances to block 352, in which the modeling compute device 120 produces, using one or models from a library of models (e.g., the models 130), one or more predictions indicative of an amount of carbon dioxide that will be removed from the atmosphere (e.g., captured through enhanced rock weathering). In doing so, the modeling compute device 120 may select one or more models 130 as a function of the obtained parameter data, as indicated in block 354. That is, the modeling compute device 120 may select one or more models 130 from the library of models as a function of a determined similarity (e.g., a similarity score, such as a calculated distance (e.g., a Euclidean distance, a cosine similarity, a result of a clustering analysis, etc.)) of the parameter data (e.g., obtained in block 302) to reference parameters for which one or more corresponding models 130 have been identified (e.g., in a data set in the memory 214 or storage 222, in a database 132, etc.) as having a high accuracy of predictions (e.g., the results 134 produced by those models have been shown to predict within a predefined threshold of accuracy (e.g., a defined percentage), actual results that were later measured in field tests). That is, if a particular model 130 is identified as more accurately predicting the amount of carbon dioxide that will be removed from the atmosphere than other models, when the parameters are similar to those obtained in block 302, the modeling compute device 120 may select that model for use.\|[0059] In some embodiments, as indicated in block 358, the modeling compute device 120 may select one or more models 130 as a function of a distance of the location where the carbon dioxide is to be captured to each of a set of reference locations associated with the models 130. That is, a data set (e.g., in the memory 214, the data storage 222, or a database 132) may identify a location (e.g., a zip code, a set of geographic coordinates, or other identifier of a location) with each model 130 in the library (e.g., because the corresponding model 130 has been shown to produce predictions with high accuracy for the associated location) and the modeling compute device 120 may select a set (e.g., one or more) of the models 130 that are closest to the location where the carbon dioxide is to be captured.\|[0060] Referring now to FIG. 5, in block 360, the modeling compute device 120 may reformat the parameter data for use by the models 130 (e.g., by converting the data into a file format that the models 130 are configured to parse (e.g., using a scripting language such as Python)). As indicated in block 362, the modeling compute device 120 may select one or more machine learning models (e.g., models, such as neural networks, decision trees, or others that may iteratively improve in prediction accuracy based on feedback). In some embodiments, the modeling compute device 120 may select an ensemble (e.g., a combination of models, in which outputs of the individual models may be weighted relative to each other), as indicated in block 364. The models 130 may include one or more models implemented by PHREEQC (e.g., PHREEQC 3), from the U.S. Geological Survey, GEM (e.g., reservoir modeling), TOUGHREACT from Lawrence Berkeley National Laboratory, and/or other models (e.g., provided by entities associated with one or more of the source compute devices 140, 142, 144). The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period, as indicated in block 366. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured each year of a defined number of years at the specified location, as indicated in block 368.\|[0061] The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per unit of area, as indicated in block 370. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per hectare, as indicated in block 372. In the illustrative embodiment, and unlike conventional systems, the modeling compute device 120 utilizes models that simulate co-precipitation of iron with toxic metals, as indicated in block 374. Additionally, and unlike conventional systems, the modeling compute device 120, in the illustrative embodiment, utilizes models that simulate basalt weathering as irreversible reactions with unidirectional rates, as indicated in block 376. Further, and unlike conventional systems, the modeling compute device 120 in the illustrative embodiment utilizes models in which near-equilibrium (e.g., within a defined percentage of an equilibrium state) rates are one to two orders of magnitude slower than far-from-equilibrium (e.g., not within the defined percentage of the equilibrium state) rates, as indicated in block 378. Further, and as indicated in block 380, the modeling compute device 120, in the illustrative embodiment, produces one or more predictions indicative of toxic metal concentrations in water associated with the location where the carbon dioxide is to be captured. In doing so, the modeling compute device 120 may produce one or more predictions indicative of concentrations of Nickel, Chromium, and/or Cadmium in the water, as indicated in block 382.\|[0062] Referring now to FIG. 6, the modeling compute device 120 may produce the one or more predications as a function of depth (e.g., depth of the water), as indicated in block 384. As indicated in block 386, the modeling compute device 120 may produce the one or more predictions regarding toxic metals in the water as a function of time (e.g., amount of toxic metals in the water per year). In some embodiments, the modeling compute device 120 may produce the predictions of toxic metals in the water relative to one or more regulations associated with the location where the carbon dioxide is to be captured, as indicated in block 388. That is, the modeling compute device 120 may obtain data (e.g., from a database 132, from a source compute device 140, 142, 144) indicative of applicable regulations and indicate whether the predicted amount of toxic metals satisfies (e.g., does not violate the regulation(s), is close to (e.g., within a defined percentage of), etc.) a limit specified by the regulations. The modeling compute device 120 may produce the prediction(s) relative to drinking water regulations and/or irrigation water regulations, as indicated in blocks 390, 392. The modeling compute device 120 may produce one or more predictions indicative of toxic metal concentrations in the soil associated with the location where the carbon dioxide is to be captured, as indicated in block 394. In doing so, the modeling compute device 120 may produce prediction(s) indicative of concentrations of Nickel, Chromium, and/or Cadmium in the soil, as indicated in block 396. The modeling compute device 120 may produce the prediction(s) as a function of depth (e.g., in the soil) and/or as a function of time, as indicated in blocks 398, 400. Similar to block 388, the modeling compute device 120 may produce the prediction(s) of toxic metals in the soil relative to one or more regulations associated with the location, as indicated in block 402.\|[0063] Referring now to FIG. 7, the modeling compute device 120 may produce data indicative of probabilities (e.g., confidence) associated with the one or more predictions, as indicated in block 404. For example, the modeling compute device 120 may produce a predictions as confidence intervals, with one prediction associated with a particular level of confidence (e.g., a percentage of likelihood), and one or more other predictions associated with other levels of confidence. As indicated in block 406, the modeling compute device 120 may determine an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. For example, the modeling compute device 120 may obtain data (e.g., from a source compute device 140, 142, 144, a database 132, etc.) indicative of a conversion rate between tons of carbon captured and a number of corresponding carbon credits and multiply the predicted amount of carbon dioxide by the conversion rate to determine the amount of carbon credits. In some embodiments, the modeling compute device 120 may adjust the number of carbon credits based on a probability or confidence level associated with the predicted amount of carbon dioxide to be removed from block 404 (e.g., by multiplying the amount of carbon dioxide by a percentage associated with the probability or confidence level). As indicated in block 408, the modeling compute device 120 may determine soil parameters that will increase capture of carbon dioxide at the location. For example, and as indicated in block 410, the modeling compute device 120 may determine, from a set of multiple basalt feed stocks, each having different mineral compositions and/or other properties, a basalt feed stock predicted to capture the most carbon dioxide in the location while maintaining compliance with regulations (e.g., toxic metals in the soil, toxic metals in the water). The modeling compute device 120 may do so by simulating carbon dioxide capture with each of the basalt feed stocks using the models 130 and identifying the basalt feed stock that satisfies the above conditions to the greatest degree.\|[0064] Continuing the method 300, the modeling compute device 120 may present a visual representation of the one or more prediction(s) in a user interface, as indicated in block 412. In the illustrative embodiment, the modeling compute device 120 produces visual presentation(s) of the prediction(s) in a web based interface (e.g., based on a HTML, JavaScript, and image data sent from the modeling compute device 120 to one or more rending engines (e.g., web browser(s)) executed by corresponding target compute devices 150, 152, 154). As indicated in block 416, in producing one or more visual representations of the prediction(s), the modeling compute device 120 may present visual representations that include interactive graphs (e.g., in which time periods, depths, or other parameters may be selected and a corresponding graph is presented). Example embodiments of visual representations 1000, 1100, 1200, 1300, 1400 of the predictions that may be presented by the modeling compute device 120 and displayed by one or more of the corresponding target compute devices 150, 152, 154 are shown in FIGS. 10-14.\|[0065] While certain illustrative embodiments have been described in detail in the drawings and the foregoing description, such an illustration and description is to be considered as exemplary and not restrictive in character, it being understood that only illustrative embodiments have been shown and described and that all changes and modifications that come within the spirit of the disclosure are desired to be protected. There exists a plurality of advantages of the present disclosure arising from the various features of the apparatus, systems, and methods described herein. It will be noted that alternative embodiments of the apparatus, systems, and methods of the present disclosure may not include all of the features described, yet still benefit from at least some of the advantages of such features. Those of ordinary skill in the art may readily devise their own implementations of the apparatus, systems, and methods that incorporate one or more of the features of the present disclosure.	(US20260017435)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/669,351 filed on Jul. 10, 2024, the disclosure of which is expressly incorporated herein.\|(US20260017435)\|BACKGROUND\|[0002] Climate change is a growing concern across the world as atmospheric greenhouse gases such as carbon dioxide trap energy radiated from the sun. While a direct result of increases in greenhouse gases is increased temperatures on Earth, knock on effects include droughts, flooding, loss of biodiversity, and disruptions in energy and transportation systems across the world. Through interactions between water and rock (e.g., in soil), carbon dioxide can be captured (e.g., removed) from the atmosphere and correspondingly lessen the effects of climate change. However, given the multitude of factors that influence the complex interactions between water and rock, it is not feasible in conventional computerized systems to reliably determine the amount of carbon dioxide that will be removed in a given location, under a given set of conditions, or to predict side effects of any efforts to enhance the capture of carbon dioxide in the soil. Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.\|SUMMARY\|[0003] The present application discloses one or more of the features recited in the appended claims and/or the following features which, alone or in any combination, may comprise patentable subject matter:\|[0004] According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may be further configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. Producing a prediction may include simulating co-precipitation of iron with one or more toxic metals. The circuitry may be further configured to present a visual representation of the at least one prediction in a user interface.\|[0005] In some embodiments, the circuitry may be configured such that using one or more models from a library of models to produce at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. The circuitry may also be configured to utilize one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, the circuitry may be configured to utilize one or more models that simulate co-precipitation of iron with toxic metals. The circuitry may be configured to obtain data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that obtaining data indicative of properties of soil includes obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and basalt mineral composition.\|[0006] The circuitry may be configured such that obtaining parameter data includes obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured to obtain parameter data as a function of an identification of the location where the carbon dioxide is to be captured by reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. The circuitry may be configured to obtain parameter data through user input into corresponding fields of a user interface. In some embodiments, the circuitry may be further configured to calculate, as a function of the obtained parameter data, additional parameter data for use by the one or more models. The circuitry may be configured such that calculating additional parameter data involves calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.\|[0007] In some embodiments, calculating additional parameter data further includes utilizing a database of specific surface areas for each of a set of minerals. The compute device, in some embodiments, may include circuitry configured to select one or more models as a function of the obtained parameter data. In some embodiments, the circuitry may be configured such that to select one or more models as a function of the obtained parameter data includes selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, the circuitry is configured such that producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. In some embodiments, the circuitry is configured such that producing at least one prediction includes reformatting the parameter data for use by the one or more models.\|[0008] The circuitry may be configured such that producing at least one prediction includes utilizing one or more machine learning models. Additionally or alternatively, the circuitry may be configured utilize an ensemble of models to produce the at least one prediction. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period. The circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, the circuitry may be configured such that to produce at least one prediction involves producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. In some embodiments, the circuitry may be configured to produce one or more predictions indicative of tons of carbon dioxide captured per hectare.\|[0009] The circuitry may be configured to produce at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, the circuitry is configured such that to produce at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time. The circuitry may be configured such that to produce the at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, the circuitry may be configured such that to produce the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions.\|[0010] In some embodiments, the circuitry may be configured such that to produce at least one prediction involves determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. The compute device, in some embodiments, may have circuitry configured such that to produce at least one prediction involves determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. In some embodiments, the circuitry may be further configured to determine, from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, the circuitry is configured such that to present a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.\|[0011] According to another aspect of the present disclosure, a method includes obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The method may further include producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering. In doing so, the method may include simulating co-precipitation of iron with one or more toxic metals. The method may further include presenting, by the compute device, a visual representation of the at least one prediction in a user interface.\|[0012] In some embodiments, producing, using one or more models from a library of models, at least one prediction includes simulating basalt weathering as irreversible reactions with unidirectional rates. Producing, using one or more models from a library of models, at least one prediction may, in some embodiments, include utilizing one or more models in which near-equilibrium rates are one to two orders of magnitude slower than far-from-equilibrium rates. In some embodiments, producing, using one or more models from a library of models, at least one prediction may include utilizing one or more models that simulate co-precipitation of iron with toxic metals. Obtaining parameter data may, in some embodiments, include obtaining data indicative of properties of soil in a location where the carbon dioxide is to be captured. In some embodiments, obtaining data indicative of properties of soil may include obtaining data indicative of minerals in the soil, carbon in the soil, effective porosity, total specific surface area, a height of a top soil layer, an amount of basalt added to the soil, basalt density, bulk soil density, and a basalt mineral composition.\|[0013] Obtaining parameter data may include obtaining the parameter data as a function of an identification of the location where the carbon dioxide is to be captured. Obtaining parameter data as a function of an identification of the location where the carbon dioxide is to be captured may include reading parameter data from a data source of properties of soil associated with location identifiers. In some embodiments, obtaining parameter data includes obtaining parameter data from a data source of mineral compositions for each of multiple basalt feed stocks. Obtaining parameter data may include obtaining parameter data through user input into corresponding fields of a user interface. The method may also include calculating, by the compute device and as a function of the obtained parameter data, additional parameter data for use by the one or more models. Calculating additional parameter data may include calculating air and blind pores, volume of soil per hectare, liters of pore water per hectare, mass of basalt per volume of soil, concentration of basalt, total weight percentage, rock specific surface area, and total surface area.\|[0014] In some embodiments, calculating additional parameter data may additionally include utilizing a database of specific surface areas for each of a set of minerals. Producing at least one prediction may include selecting one or more models as a function of the obtained parameter data. Selecting one or more models as a function of the obtained parameter data may involve selecting one or more models as a function of a determined similarity of the parameter data to reference parameters for which a corresponding model is identified as having an accuracy that satisfies a defined threshold. In some embodiments, producing at least one prediction includes selecting one or more models as a function of a distance of a location where the carbon dioxide is to be captured from one or more reference locations associated with the models in the library. Producing at least one prediction may include reformatting the parameter data for use by the one or more models. In some embodiments, producing at least one prediction involves utilizing one or more machine learning models. Producing at least one prediction may, in some embodiments, include utilizing an ensemble of models to produce the at least one prediction. Producing at least one prediction may include producing one or more predictions indicative of tons of carbon dioxide captured over a predefined time period.\|[0015] Producing one or more predictions may include producing one or more predictions indicative of tons of carbon dioxide captured each year over a defined number of years. In some embodiments, producing at least one prediction includes producing one or more predictions indicative of tons of carbon dioxide captured per unit of area. Producing one or more predictions may, in some embodiments, include producing one or more predictions indicative of tons of carbon dioxide captured per hectare. In some embodiments, producing at least one prediction includes producing at least one prediction indicative of toxic metal concentrations in water associated with a location where the carbon dioxide is to be captured. Producing at least one prediction indicative of toxic metal concentrations in water may, in some embodiments, involve producing at least one prediction of concentrations of Nickel, Chromium, and Cadmium in the water. In some embodiments, producing at least one prediction indicative of toxic metal concentrations in water involves producing the at least one prediction as a function of depth and time.\|[0016] Producing the at least one prediction indicative of toxic metal concentrations in water may involve producing the at least one prediction relative to one or more regulations pertaining to drinking water or irrigation water associated with the location where the carbon dioxide is to be captured. In some embodiments, producing the at least one prediction involves producing data indicative of a probability or confidence associated with each of multiple predictions. Producing at least one prediction may include determining an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. In some embodiments, producing at least one prediction includes determining soil parameters to increase capture of carbon dioxide from the atmosphere at a location. The method may also include determining, by the compute device and from a set of multiple basalt feed stocks, a basalt feed stock predicted to capture the most carbon dioxide at the location while maintaining compliance with one or more regulations associated with the location. In some embodiments, presenting a visual representation of the at least one prediction in a user interface involves presenting a visual representation of the at least one prediction in a web-based interface that includes interactive graphs.\|[0017] According to another aspect of the present disclosure, one or more machine-readable storage media may include instructions stored thereon that, in response to being executed, cause a compute device to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The instructions may further cause the compute device to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Additionally, the instructions may cause the compute device to present a visual representation of the at least one prediction in a user interface. Further, the instructions may cause the compute device to perform any of the methods described above.\|[0018] Additional features, which alone or in combination with any other feature(s), such as those listed above and/or those listed in the claims, may comprise patentable subject matter and will become apparent to those skilled in the art upon consideration of the following detailed description of various embodiments exemplifying the best mode of carrying out the embodiments as presently perceived.\|(US20260017435)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0019] The concepts described herein are illustrated by way of example and not by way of limitation in the accompanying figures. For simplicity and clarity of illustration, elements illustrated in the figures are not necessarily drawn to scale. Where considered appropriate, reference labels have been repeated among the figures to indicate corresponding or analogous elements. The detailed description particularly refers to the accompanying figures in which:\|[0020] FIG. 1 is a simplified block diagram of at least one embodiment of a system for modeling carbon dioxide removal through enhanced rock weathering;\|[0021] FIG. 2 is a simplified block diagram of at least one embodiment of a compute device of the system of FIG. 1;\|[0022] FIGS. 3-7 are flowcharts of at least one embodiment of a method for modeling carbon dioxide removal through enhanced rock weathering that may be performed by the system of FIG. 1;\|[0023] FIGS. 8 and 9 are user interfaces that may be produced by the system of FIG. 1; and\|[0024] FIG. 10 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating carbon capture as a function of years;\|[0025] FIG. 11 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating a simulation of carbon capture as a function of time;\|[0026] FIG. 12 is one embodiment of visual representations of the predictions that may be presented by the modeling compute device of the system of FIG. 1, illustrating the confidence interval of the simulations over a five year period;\|[0027] FIG. 13 is one embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1; and\|[0028] FIG. 14 is another embodiment of visual representations of nickel presence as a function of soil depth as presented by the modeling compute device of the system of FIG. 1;\|(US20260017435)\|DETAILED DESCRIPTION OF THE DRAWINGS\|[0029] While the concepts of the present disclosure are susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and will be described herein in detail. It should be understood, however, that there is no intent to limit the concepts of the present disclosure to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives consistent with the present disclosure and the appended claims.\|[0030] References in the specification to “one embodiment,” “an embodiment,” “an illustrative embodiment,” etc., indicate that the embodiment described may include a particular feature, structure, or characteristic, but every embodiment may or may not necessarily include that particular feature, structure, or characteristic. Moreover, such phrases are not necessarily referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with an embodiment, it is submitted that it is within the knowledge of one skilled in the art to effect such feature, structure, or characteristic in connection with other embodiments whether or not explicitly described. Additionally, it should be appreciated that items included in a list in the form of “at least one A, B, and C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C). Similarly, items listed in the form of “at least one of A, B, or C” can mean (A); (B); (C); (A and B); (A and C); (B and C); or (A, B, and C).\|[0031] The disclosed embodiments may be implemented, in some cases, in hardware, firmware, software, or any combination thereof. The disclosed embodiments may also be implemented as instructions carried by or stored on a transitory or non-transitory machine-readable (e.g., computer-readable) storage medium, which may be read and executed by one or more processors. A machine-readable storage medium may be embodied as any storage device, mechanism, or other physical structure for storing or transmitting information in a form readable by a machine (e.g., a volatile or non-volatile memory, a media disc, or other media device).\|[0032] In the drawings, some structural or method features may be shown in specific arrangements and/or orderings. However, it should be appreciated that such specific arrangements and/or orderings may not be required. Rather, in some embodiments, such features may be arranged in a different manner and/or order than shown in the illustrative figures. Additionally, the inclusion of a structural or method feature in a particular figure is not meant to imply that such feature is required in all embodiments and, in some embodiments, may not be included or may be combined with other features.\|[0033] Referring now to FIG. 1, a system 100 for modeling carbon dioxide removal through enhanced rock weathering includes a set of one or more modeling compute devices 120, a set of source compute devices 140, 142, 144 and a set of target compute devices 150, 152, 154. In operation, the modeling compute devices 120 operate as a gateway 110 through which end users (e.g., scientists, organizations, etc.) of operating target compute devices 150, 152, 154 may view predictions (e.g., forecasts) of how much carbon dioxide will be captured in the soil at a particular location through a process of enhanced rock weathering. In enhanced rock weathering, rock, such as basalt, is added to soil at a location (e.g., one or more hectares of land) in a powdered form to increase the amount of carbon dioxide removed from the atmosphere through interaction between the carbon dioxide, water (e.g., rain), and rock. The composition of the basalt (e.g., mineral composition) as well as properties of the soil itself (e.g., porosity, carbon content, minerals, etc.) influence the amount of carbon dioxide that will be captured and may impact an amount of toxic metals present in the soil and/or water in the location as a result of the chemical processes involved in the capture of the carbon dioxide. As such, given the multitude of factors that can influence the amount of carbon dioxide removal, the modeling compute devices 120 may utilize a library of models 130 (e.g., thousands of models) and a database 132 of properties of minerals that also affect the amount of carbon dioxide that will be captured. The modeling compute devices 120 produce results 134, which may be embodied as data indicative of amount of carbon dioxide that will be captured under the specified conditions. Additionally, the results 134 may indicate the amount of toxic metals that are predicted to be present in the soil and water as a result of the chemical processes. Further, the results may be broken down across multiple years, depths, confidence intervals, or other parameters and may be the product of thousands of simulations using the set of models 130.\|[0034] The source compute devices 140, 142, 144 may provide data indicative of properties of the soil in various locations, properties of basalt (e.g., various feed stocks of basalt), information indicative of a carbon credits market (e.g., an amount of carbon credits associated with an amount of carbon captured or removed from the atmosphere), data indicative of regulations associated with various locations (e.g., drinking water regulations, irrigation water regulations, soil regulations), and/or other data usable by the modeling compute devices 120 in simulating the capture of carbon from the atmosphere through enhanced rock weathering processes.\|[0035] In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. The system 100, in operation, provides innovative and independent geochemical models and modeling forecasts, filling a current gap in monitoring, reporting, and verification (MRV). Further, the system 100 contributes to the trust that is necessary for the scale-up of climate-tech carbon dioxide removal (CDR) industries to the gigaton level. While the system 100, in some embodiments, focuses on enhanced rock weathering, the science and technologies can also be applied to storing carbon dioxide in basalt and sandstone aquifers and mine tailings.\|[0036] A modeling forecast is useful at every stage of a project: conceptualization, contract negotiation, application, and post-project monitoring. The gateway 110, in the illustrative embodiment, is cloud-based, documented, and based on advanced cyberinfrastructure and data sciences that transform how modeling is delivered and how results are archived, analyzed, and presented. The gateway 110, in the illustrative embodiment, provides industry-standard authentication, authorization, and controlled sharing capabilities. Further, the system 100 provides provenance for the execution of tools, clonability, and reusability and integrates with national open cyberinfrastructure and public clouds for workflow execution.\|[0037] In the illustrative embodiment, the gateway 110 may serve four types of clients: a) technical specialists at stakeholders (CDR and purchaser corporations, regulatory agencies, environmental groups) who can search a large library of models 130 to find the likely outcomes for their projects; b) geochemical experts who can develop or tweak their models 130 on the gateway 110, but aided by automatic documentation, archives, and traceability on the gateway; c) stakeholders with no in-house capabilities who wish to outsource the initial development of models 130 and run the models 130 on the gateway 110; d) stakeholders who need independent models as certification. The availability of the gateway 110 may operate to broaden the participation of underrepresented groups and less developed countries, helping achieve the common goal of implementing scalable solutions around the world.\|[0038] Enhanced rock weathering can be generally represented with the equations shown below:\|[0039] Other equations representative of geochemical reactions are set forth in “Environmental Applications of Geochemical Modeling” by Chen Zhu and Greg Anderson, published in 2002, the contents of which are incorporated herein by reference. As discussed herein, characteristics of the soil and basalt in the soil can significantly impact the amount of carbon dioxide that will be captured and the amounts of metals (e.g., toxic metals) that may be introduced into the soil and water through the enhanced rock wreathing process. The models 130, in the illustrative embodiment, account for the characteristics through parameters discussed herein. Further, the models 130 incorporate features that are not present in conventional modeling systems, including the following: a. Near-equilibrium rates (e.g., in systems with relatively low Gibbs energy) are modeled to be one to two orders of magnitude slower than the far-from-equilibrium rates (e.g., in systems with relatively high Gibbs energy), rather than the far-from-equilibrium rate constants used in other models; b. basalt weathering is simulated as irreversible reactions with unidirectional rates (not reversible reactions in other models, which are theoretically wrong); and c. the models 130 include co-precipitation of toxic metals released from enhanced rock weathering with iron oxyhydroxides. Without co-precipitation in the models 130, the forecasts of toxic metal released into soil may incorrectly indicate toxic metal amounts in excess of applicable regulations. The models 130 may be fine-tuned with time, and more components may be added to the model 130.\|[0040] Further, the system 100, in the illustrative embodiment, provides a web-based model interface. Geochemical models are generally inaccessible to non-experts and the number of experts in the world is in short supply. The system 100 leverages expertise and experience of experts and makes modeling and modeling results available to non-experts. The gateway 110, in the illustrative embodiment, utilizes a database (e.g., the database 132) of mineralogical compositions of basalt feed stocks to be applied to croplands, and provides a web tool (e.g., a web based user interface) that allows users to input mineralogical compositions of the specific feed stock. Behind the web interface, the gateway 110 utilizes a database (e.g., the database 132) of different specific surface areas for different minerals. In operation, the gateway 110 may perform automatic input file generation (e.g., reformatting of parameter data into a format usable by the models 130).\|[0041] The web interface and models enable users (e.g., operating the target compute devices 150, 152, 154) to combine different parameters and run different scenarios to view resulting predictions of carbon capture through enhanced rock weathering and side effects thereof. For example, users may compare how much carbon dioxide is captured by applying 100 tons of basalt per hectare versus ten tons of basalt per hectare, and using one feed stock of basalt (e.g., Oregon basalt) versus another feed stock of basalt (e.g., Columbia River basalt). Users may also view the differences in carbon capture given different particle sizes. Further, users may view data that is indicative of toxic metal release into water and soil under varying conditions.\|[0042] In the illustrative embodiment, the gateway 110 may maintain a library of millions of simulations with a wide range of field conditions. The library may be searchable and the gateway 110 may enable users to locate modeling results and graphic presentations that fit their field conditions within minutes, rather than waiting for hours or longer for simulation results. The library may serve as a base for development or improvement of machine learning algorithms to (1) accelerate the simulations; and (2) find patterns, which lead to faster, more accurate, and more interpretable models. The models 130, in the illustrate embodiment, are calibrated geochemical models that bridge the gap between laboratory and field-based estimates of geochemical reactions. In particular, the models 130 may be calibrated with enhanced rock weathering batch scale laboratory experimental data, field data, and lysimeter experimental data. The results 134 may be embodied as databases and input files with adjusted parameters or semi-empirical scaling factors. In effect, the gateway 110 may provide independent, rigorous, models and modeling results that come with trust and creditability.\|[0043] While a relatively small number of compute devices 120, 140, 142, 144, 150, 152, 154 are shown in FIG. 1 for simplicity and clarity, it should be understood that the number of compute devices, in practice, may range in the tens, hundreds, thousands, or more. Likewise, it should be understood that the compute devices 120, 140, 142, 144, 150, 152, 154 may be distributed differently or perform different roles than the configuration shown in FIG. 1. Further, though shown as separate compute devices 120, 140, 142, 144, 150, 152, 154 in some embodiments, the functionality of one or more of the compute devices 120, 140, 142, 144, 150, 152, 154 may be combined into fewer compute devices and/or distributed across more compute devices than those shown in FIG. 1.\|[0044] Referring now to FIG. 2, an illustrative embodiment of a modeling compute device 120 includes a compute engine 210, an input/output (I/O) subsystem 216, communication circuitry 218, and one or more data storage devices 222. In some embodiments, the modeling compute device 120 may include one or more display devices 224 and/or one or more peripheral devices 226 (e.g., a mouse, a physical keyboard, etc.). In some embodiments, one or more of the illustrative components may be incorporated in, or otherwise form a portion of, another component. The compute engine 210 may be embodied as any type of device or collection of devices capable of performing various compute functions described below. In some embodiments, the compute engine 210 may be embodied as a single device such as an integrated circuit, an embedded system, a field-programmable gate array (FPGA), a system-on-a-chip (SOC), or other integrated system or device. Additionally, in the illustrative embodiment, the compute engine 210 includes or is embodied as a processor 212 and a memory 214. The processor 212 may be embodied as any type of processor capable of performing the functions described herein. For example, the processor 212 may be embodied as a single or multi-core processor(s), a microcontroller, or other processor or processing/controlling circuit. In some embodiments, the processor 212 may be embodied as, include, or be coupled to an FPGA, an application specific integrated circuit (ASIC), reconfigurable hardware or hardware circuitry, or other specialized hardware to facilitate performance of the functions described herein.\|[0045] In embodiments, the processor 212 is capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, a set of instructions which when executed by the processor 212 cause the modeling compute device 120 to perform one or more operations described herein. In embodiments, the processor 212 is further capable of receiving, e.g., from the memory 214 or via the I/O subsystem 216, one or more signals from external sources, e.g., from the peripheral devices 226 or via the communication circuitry 218 from an external compute device, external source, or external network. As one will appreciate, a signal may contain encoded instructions and/or information. In embodiments, once received, such a signal may first be stored, e.g., in the memory 214 or in the data storage device(s) 222, thereby allowing for a time delay in the receipt by the processor 212 before the processor 212 operates on a received signal. Likewise, the processor 212 may generate one or more output signals, which may be transmitted to an external device, e.g., an external memory or an external compute engine via the communication circuitry 218 or, e.g., to one or more display devices 224. In some embodiments, a signal may be subjected to a time shift in order to delay the signal. For example, a signal may be stored on one or more storage devices 222 to allow for a time shift prior to transmitting the signal to an external device. One will appreciate that the form of a particular signal will be determined by the particular encoding a signal is subject to at any point in its transmission (e.g., a signal stored will have a different encoding than a signal in transit, or, e.g., an analog signal will differ in form from a digital version of the signal prior to an analog-to-digital (A/D) conversion).\|[0046] The main memory 214 may be embodied as any type of volatile (e.g., dynamic random access memory (DRAM), etc.) or non-volatile memory or data storage capable of performing the functions described herein. Volatile memory may be a storage medium that requires power to maintain the state of data stored by the medium. In some embodiments, all or a portion of the main memory 214 may be integrated into the processor 212. In operation, the main memory 214 may store various software and data used during operation such as models, databases, simulation results, applications, libraries, and drivers.\|[0047] The compute engine 210 is communicatively coupled to other components of the modeling compute device 120 via the I/O subsystem 216, which may be embodied as circuitry and/or components to facilitate input/output operations with the compute engine 210 (e.g., with the processor 212 and the main memory 214) and other components of the modeling compute device 120. For example, the I/O subsystem 216 may be embodied as, or otherwise include, memory controller hubs, input/output control hubs, integrated sensor hubs, firmware devices, communication links (e.g., point-to-point links, bus links, wires, cables, light guides, printed circuit board traces, etc.), and/or other components and subsystems to facilitate the input/output operations. In some embodiments, the I/O subsystem 216 may form a portion of a system-on-a-chip (SoC) and be incorporated, along with one or more of the processor 212, the main memory 214, and other components of the modeling compute device 120, into the compute engine 210.\|[0048] The communication circuitry 218 may be embodied as any communication circuit, device, or collection thereof, capable of enabling communications over a network between the modeling compute device 120 and another device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). The communication circuitry 218 may be configured to use any one or more communication technology (e.g., wired or wireless communications) and associated protocols (e.g., Ethernet, Wi-Fi®, WiMAX, Bluetooth®, etc.) to effect such communication.\|[0049] The illustrative communication circuitry 218 includes a network interface controller (NIC) 220. The NIC 220 may be embodied as one or more add-in-boards, daughter cards, network interface cards, controller chips, chipsets, or other devices that may be used by the modeling compute device 120 to connect with another compute device (e.g., a compute device 140, 142, 144, 150, 152, 154, etc.). In some embodiments, the NIC 220 may be embodied as part of a system-on-a-chip (SoC) that includes one or more processors, or included on a multichip package that also contains one or more processors. In some embodiments, the NIC 220 may include a local processor (not shown) and/or a local memory (not shown) that are both local to the NIC 220. Additionally or alternatively, in such embodiments, the local memory of the NIC 220 may be integrated into one or more components of the modeling compute device 120 at the board level, socket level, chip level, and/or other levels.\|[0050] Each data storage device 222, may be embodied as any type of device configured for short-term or long-term storage of data such as, for example, memory devices and circuits, memory cards, hard disk drives, solid-state drives, or other data storage device. Each data storage device 222 may include a system partition that stores data and firmware code for the data storage device 222 and one or more operating system partitions that store data files and executables for operating systems.\|[0051] Each display device 224 may be embodied as any device or circuitry (e.g., a liquid crystal display (LCD), a light emitting diode (LED) display, a cathode ray tube (CRT) display, etc.) configured to display visual information (e.g., text, graphics, etc.) to a user. In some embodiments, a display device 224 may be embodied as a touch screen (e.g., a screen incorporating resistive touchscreen sensors, capacitive touchscreen sensors, surface acoustic wave (SAW) touchscreen sensors, infrared touchscreen sensors, optical imaging touchscreen sensors, acoustic touchscreen sensors, and/or other type of touchscreen sensors) to detect selections of on-screen user interface elements or gestures from a user.\|[0052] In the illustrative embodiment, the components of the modeling compute device 120 are housed in a single unit. However, in other embodiments, the components may be in separate housings, in separate racks of a data center, and/or spread across multiple data centers or other facilities. The compute devices 140, 142, 144, 150, 152, 154 may have components similar to those described in FIG. 2 with reference to the modeling compute device 120. The description of those components of the modeling compute device 120 is equally applicable to the description of components of the compute devices 140, 142, 144, 150, 152, 154. Further, it should be appreciated that any of the devices 120, 140, 142, 144, 150, 152, 154 may include other components, sub-components, and devices commonly found in a computing device, which are not discussed above in reference to the modeling compute device 120 and not discussed herein for clarity of the description.\|[0053] In the illustrative embodiment, the compute devices 120, 140, 142, 144, 150, 152, 154 are in communication via a network 160, which may be embodied as any type of wired or wireless communication network, including global networks (e.g., the internet), wide area networks (WANs), local area networks (LANs), digital subscriber line (DSL) networks, cable networks (e.g., coaxial networks, fiber networks, etc.), cellular networks (e.g., Global System for Mobile Communications (GSM), Long Term Evolution (LTE), Worldwide Interoperability for Microwave Access (WiMAX), 3G, 4G, 5G, etc.), a radio area network (RAN), or any combination thereof.\|[0054] Referring now to FIG. 3, the system 100 (e.g., a modeling compute device 120 of the gateway 110) may perform a method 300 for modeling carbon dioxide removal through enhanced rock weathering. The method 300, in the illustrative embodiment, begins with block 302 in which the modeling compute device 120 obtains parameter data indicative of parameters for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering (e.g., the application of basalt dust to soil to increase the amount of carbon dioxide captured through the interaction of water (e.g., rain), carbon dioxide, and rock (e.g., the basalt dust)). In doing so, and as indicated in block 304, the modeling compute device 120 obtains data indicative of properties of soil in a location where the carbon dioxide is to be captured (e.g., removed from the atmosphere through enhanced rock weathering). In the illustrative embodiment, the modeling compute device 120 may obtain data indicative of minerals in the soil (e.g., a numeric value, such as a number indicative of a percentage of the soil comprising minerals), as indicated in block 306. As indicated in block 308, the modeling compute device 120 may obtain data indicative of carbon in the soil (e.g., a numeric value indicative of a percentage of the soil comprising carbon).\|[0055] The modeling compute device 120 may additionally obtain data indicative of effective porosity of the soil where the carbon is to be captured, as indicated in block 310. The effective porosity may be expressed, in at least some embodiments, as a numeric value (e.g., a percentage). As indicated in block 312, the modeling compute device 120 may obtain parameter data indicative of total specific surface area. In at least some embodiments, the total specific surface area may be expressed as square meters per gram. The modeling compute device 120 may obtain data indicative of the height of a top soil layer, as indicated in block 314. The height, in the illustrative embodiment, is expressed in meters. Further, the modeling compute device 120 may obtain data indicative of an amount of basalt added to the soil (e.g., tons per hectare), as indicated in block 316. Further, the modeling compute device 120 may obtain data indicative of basalt density, such as in grams per cubic centimeter, as indicated in block 318. Additionally, the modeling compute device 120 may obtain data indicative of bulk soil density, as indicated in block 320. The bulk soil density, in at least some embodiments, may be expressed as grams per cubic centimeter. The modeling compute device 120 may also obtain data indicative of basalt mineral composition, as indicated in block 322. The mineral composition of the basalt may be structured as one or more pairs of values, with each pair including an identifier (e.g., name, abbreviation, etc.) of a mineral and a corresponding percentage (e.g., indicative of a percentage of the basalt feed stock that the mineral constitutes).\|[0056] Still referring to FIG. 3, the modeling compute device 120 may obtain the parameter data as a function of (e.g., based on) an identification of the location where the carbon dioxide is to be captured in the soil, as indicated in block 324. In doing so, the modeling compute device 120 may read parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of properties of soil associated with location identifiers (e.g., plot numbers, geographic coordinates, zip codes, etc.), as indicated in block 326. In some embodiments, the modeling compute device 120 may obtain parameter data from a data source (e.g., a database 132, a data set transmitted from a source compute device 140, 142, 144, etc.) of mineral compositions from each of multiple basalt feed stocks, as indicated in block 328. Additionally or alternatively, the modeling compute device 120 may obtain parameter data through user input into corresponding fields (e.g., text boxes, check boxes, etc.) of a user interface (e.g., a graphical user interface presented by a target compute device 150, 152, 154 based on code (e.g., hypertext markup language (HTML) and/or JavaScript) and images (e.g., portable network graphics (PNG) files, Joint Photographic Experts Group (JPEG) files, or the like) transmitted from the modeling compute device 120 to the target compute device(s) 150, 152, 154 via the network 160, as indicated in block 330. An embodiment of a user interface 800 with which the modeling compute device 120 may obtain parameter data is shown in FIG. 8. The user interface 800 includes a first screen 810 that comprises parameter data about soil properties and a second screen 820 that includes parameter data about basalt mineral makeup. The user interface 800 provides one embodiment that users can use to input parameters related to soil properties and basalt mineral composition, run the models, and calculate how much CO2 can be sequestered.\|[0057] Referring now to FIG. 4, the method 300 continues in block 332 in which the modeling compute device 120 may calculate, as a function of the obtained parameter data, additional parameter data for use by one or more models (e.g., the models 130). In doing so, the modeling compute device 120 may calculate air and blind pores (e.g., a numeric value), as indicated in block 334. The modeling compute device 120 may additionally calculate a volume of soil per hectare, as indicated in block 336. Further, the modeling compute device 120 may calculate a number of volume (e.g., liters) of pore water per unit of area (e.g., hectare), as indicated in block 338. Additionally, the modeling compute device 120 may calculate a mass of basalt per unit of volume of the soil, as indicated in block 340. In addition, the modeling compute device 120 may calculate a concentration of basalt in the soil, as indicated in block 342. Further, the modeling compute device 120 may calculate a total weight percentage, as indicated in block 344. The modeling compute device 120 may also calculate a rock specific surface area, as indicated in block 346. In addition, the modeling compute device 120 may calculate a total surface area, in block 348. In performing the calculations, the modeling compute device 120 may utilize a database (e.g., a database 132) of specific surface areas for each of a set of minerals (e.g., minerals in the soil, in the basalt, etc.), as indicated in block 350. An embodiment of a user interface 900 in which the modeling compute device 120 may display additional parameters calculated as discussed above is shown in FIG. 9. In some embodiments, the user interface 800 includes a third screen 830 that may display additional parameters calculated as discussed above.\|[0058] After obtaining the parameter data, the method 300, in the illustrative embodiment, advances to block 352, in which the modeling compute device 120 produces, using one or models from a library of models (e.g., the models 130), one or more predictions indicative of an amount of carbon dioxide that will be removed from the atmosphere (e.g., captured through enhanced rock weathering). In doing so, the modeling compute device 120 may select one or more models 130 as a function of the obtained parameter data, as indicated in block 354. That is, the modeling compute device 120 may select one or more models 130 from the library of models as a function of a determined similarity (e.g., a similarity score, such as a calculated distance (e.g., a Euclidean distance, a cosine similarity, a result of a clustering analysis, etc.)) of the parameter data (e.g., obtained in block 302) to reference parameters for which one or more corresponding models 130 have been identified (e.g., in a data set in the memory 214 or storage 222, in a database 132, etc.) as having a high accuracy of predictions (e.g., the results 134 produced by those models have been shown to predict within a predefined threshold of accuracy (e.g., a defined percentage), actual results that were later measured in field tests). That is, if a particular model 130 is identified as more accurately predicting the amount of carbon dioxide that will be removed from the atmosphere than other models, when the parameters are similar to those obtained in block 302, the modeling compute device 120 may select that model for use.\|[0059] In some embodiments, as indicated in block 358, the modeling compute device 120 may select one or more models 130 as a function of a distance of the location where the carbon dioxide is to be captured to each of a set of reference locations associated with the models 130. That is, a data set (e.g., in the memory 214, the data storage 222, or a database 132) may identify a location (e.g., a zip code, a set of geographic coordinates, or other identifier of a location) with each model 130 in the library (e.g., because the corresponding model 130 has been shown to produce predictions with high accuracy for the associated location) and the modeling compute device 120 may select a set (e.g., one or more) of the models 130 that are closest to the location where the carbon dioxide is to be captured.\|[0060] Referring now to FIG. 5, in block 360, the modeling compute device 120 may reformat the parameter data for use by the models 130 (e.g., by converting the data into a file format that the models 130 are configured to parse (e.g., using a scripting language such as Python)). As indicated in block 362, the modeling compute device 120 may select one or more machine learning models (e.g., models, such as neural networks, decision trees, or others that may iteratively improve in prediction accuracy based on feedback). In some embodiments, the modeling compute device 120 may select an ensemble (e.g., a combination of models, in which outputs of the individual models may be weighted relative to each other), as indicated in block 364. The models 130 may include one or more models implemented by PHREEQC (e.g., PHREEQC 3), from the U.S. Geological Survey, GEM (e.g., reservoir modeling), TOUGHREACT from Lawrence Berkeley National Laboratory, and/or other models (e.g., provided by entities associated with one or more of the source compute devices 140, 142, 144). The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide captured over a predefined time period, as indicated in block 366. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured each year of a defined number of years at the specified location, as indicated in block 368.\|[0061] The modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per unit of area, as indicated in block 370. In doing so, the modeling compute device 120 may produce one or more predictions indicative of tons of carbon dioxide that will be captured per hectare, as indicated in block 372. In the illustrative embodiment, and unlike conventional systems, the modeling compute device 120 utilizes models that simulate co-precipitation of iron with toxic metals, as indicated in block 374. Additionally, and unlike conventional systems, the modeling compute device 120, in the illustrative embodiment, utilizes models that simulate basalt weathering as irreversible reactions with unidirectional rates, as indicated in block 376. Further, and unlike conventional systems, the modeling compute device 120 in the illustrative embodiment utilizes models in which near-equilibrium (e.g., within a defined percentage of an equilibrium state) rates are one to two orders of magnitude slower than far-from-equilibrium (e.g., not within the defined percentage of the equilibrium state) rates, as indicated in block 378. Further, and as indicated in block 380, the modeling compute device 120, in the illustrative embodiment, produces one or more predictions indicative of toxic metal concentrations in water associated with the location where the carbon dioxide is to be captured. In doing so, the modeling compute device 120 may produce one or more predictions indicative of concentrations of Nickel, Chromium, and/or Cadmium in the water, as indicated in block 382.\|[0062] Referring now to FIG. 6, the modeling compute device 120 may produce the one or more predications as a function of depth (e.g., depth of the water), as indicated in block 384. As indicated in block 386, the modeling compute device 120 may produce the one or more predictions regarding toxic metals in the water as a function of time (e.g., amount of toxic metals in the water per year). In some embodiments, the modeling compute device 120 may produce the predictions of toxic metals in the water relative to one or more regulations associated with the location where the carbon dioxide is to be captured, as indicated in block 388. That is, the modeling compute device 120 may obtain data (e.g., from a database 132, from a source compute device 140, 142, 144) indicative of applicable regulations and indicate whether the predicted amount of toxic metals satisfies (e.g., does not violate the regulation(s), is close to (e.g., within a defined percentage of), etc.) a limit specified by the regulations. The modeling compute device 120 may produce the prediction(s) relative to drinking water regulations and/or irrigation water regulations, as indicated in blocks 390, 392. The modeling compute device 120 may produce one or more predictions indicative of toxic metal concentrations in the soil associated with the location where the carbon dioxide is to be captured, as indicated in block 394. In doing so, the modeling compute device 120 may produce prediction(s) indicative of concentrations of Nickel, Chromium, and/or Cadmium in the soil, as indicated in block 396. The modeling compute device 120 may produce the prediction(s) as a function of depth (e.g., in the soil) and/or as a function of time, as indicated in blocks 398, 400. Similar to block 388, the modeling compute device 120 may produce the prediction(s) of toxic metals in the soil relative to one or more regulations associated with the location, as indicated in block 402.\|[0063] Referring now to FIG. 7, the modeling compute device 120 may produce data indicative of probabilities (e.g., confidence) associated with the one or more predictions, as indicated in block 404. For example, the modeling compute device 120 may produce a predictions as confidence intervals, with one prediction associated with a particular level of confidence (e.g., a percentage of likelihood), and one or more other predictions associated with other levels of confidence. As indicated in block 406, the modeling compute device 120 may determine an amount of carbon credits associated with the predicted amount of carbon dioxide to be removed from the atmosphere. For example, the modeling compute device 120 may obtain data (e.g., from a source compute device 140, 142, 144, a database 132, etc.) indicative of a conversion rate between tons of carbon captured and a number of corresponding carbon credits and multiply the predicted amount of carbon dioxide by the conversion rate to determine the amount of carbon credits. In some embodiments, the modeling compute device 120 may adjust the number of carbon credits based on a probability or confidence level associated with the predicted amount of carbon dioxide to be removed from block 404 (e.g., by multiplying the amount of carbon dioxide by a percentage associated with the probability or confidence level). As indicated in block 408, the modeling compute device 120 may determine soil parameters that will increase capture of carbon dioxide at the location. For example, and as indicated in block 410, the modeling compute device 120 may determine, from a set of multiple basalt feed stocks, each having different mineral compositions and/or other properties, a basalt feed stock predicted to capture the most carbon dioxide in the location while maintaining compliance with regulations (e.g., toxic metals in the soil, toxic metals in the water). The modeling compute device 120 may do so by simulating carbon dioxide capture with each of the basalt feed stocks using the models 130 and identifying the basalt feed stock that satisfies the above conditions to the greatest degree.\|[0064] Continuing the method 300, the modeling compute device 120 may present a visual representation of the one or more prediction(s) in a user interface, as indicated in block 412. In the illustrative embodiment, the modeling compute device 120 produces visual presentation(s) of the prediction(s) in a web based interface (e.g., based on a HTML, JavaScript, and image data sent from the modeling compute device 120 to one or more rending engines (e.g., web browser(s)) executed by corresponding target compute devices 150, 152, 154). As indicated in block 416, in producing one or more visual representations of the prediction(s), the modeling compute device 120 may present visual representations that include interactive graphs (e.g., in which time periods, depths, or other parameters may be selected and a corresponding graph is presented). Example embodiments of visual representations 1000, 1100, 1200, 1300, 1400 of the predictions that may be presented by the modeling compute device 120 and displayed by one or more of the corresponding target compute devices 150, 152, 154 are shown in FIGS. 10-14.\|[0065] While certain illustrative embodiments have been described in detail in the drawings and the foregoing description, such an illustration and description is to be considered as exemplary and not restrictive in character, it being understood that only illustrative embodiments have been shown and described and that all changes and modifications that come within the spirit of the disclosure are desired to be protected. There exists a plurality of advantages of the present disclosure arising from the various features of the apparatus, systems, and methods described herein. It will be noted that alternative embodiments of the apparatus, systems, and methods of the present disclosure may not include all of the features described, yet still benefit from at least some of the advantages of such features. Those of ordinary skill in the art may readily devise their own implementations of the apparatus, systems, and methods that incorporate one or more of the features of the present disclosure.	Family Number\|(117356463)\|117356463\|Object of Invention\|(US20260017435 A1)\| (...) the following features which, alone or in any combination, may comprise patentable subject matter:According to an aspect of the present disclosure, a compute device may include circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering.\|In the illustrative embodiment, the system 100 provides a science gateway (e.g., the gateway 110) for forecasting the efficacy of enhanced rock weathering, predicting and quantifying carbon dioxide removal as well as toxic metal release into waters and soils. \|Abstract\|(US20260017435 A1)\|Technologies for modeling carbon dioxide removal include a compute device with circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may also be configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Further, the circuitry may be configured to present a visual representation of the at least one prediction in a user interface. Other embodiments are also described and claimed.\|Title\|(US20260017435 A1)\|Technologies for modeling carbon dioxide removal\|Advantages / Prev. Drawbacks\|(US20260017435 A1)\|Likewise, conventional systems do not reliably enable a determination of what factors will enable the largest amount of carbon dioxide removal in a given location in the world while satisfying concerns about possible side effects of efforts to enhance the removal of carbon dioxide.\|Independent Claims\|(US20260017435 A1)\| (...) obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| (...) obtaining, by a compute device, parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; producing, by the compute device and using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\| (...) obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering; produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals; and\|	Computer technology\|Environmental technology	B01D-053/62\|B01D-053/82\|B01D-2257/504\|G06F-030/27		B01D-053/62\|B01D-053/82\|B01D-2257/504\|G06F-030/27	B01D-053/62\|B01D-053/82\|G06F-030/27	B01D-053/62\|B01D-053/82\|G06F-030/27										PENDING	(US20260017435)\|PENDING	ALIVE	(US20260017435)\|ALIVE	(US20260017435)\|LEGAL DETAILS FOR US20260017435\|Actual or expected expiration date=2045-07-09\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-07-09\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19264502\|Application date=2025-07-09\|Standardized application number=2025US-19264502\|Event publication date=2025-07-09\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-07-09\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-07-09\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 29920-426689\|Event publication date=2025-07-09\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 138060\|Event publication date=2025-07-09\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2025-07-09\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-07-09\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-07-25\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2025-07-29\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-09-29\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-10-02\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2025-10-22\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-10-22\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2026-01-15\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20260017435\|Publication stage code=A1\|Publication date=2026-01-15\|Standardized publication number=US20260017435\|Event publication date=2026-01-16\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification		(US20260017435)\|US	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcP7LGmymc8G11q5LJ03xVJIJjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023247689&ekey=1952&xpn=US20260017435&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19264502/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=rCUZBbi%252Bv%252B%252FyiDX9GDUoPcRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(US20260017435)\|US	(US20260017435)\|NAME=THE TRUSTEES OF INDIANA UNIVERSITY , CITY=Bloomington , STATE=IN , COUNTRY=US			(US20260017435)\|US	(US20260017435)\|NAME=Zhu Chen, CITY=Bloomington, STATE=IN , COUNTRY=US	(US20260017435)\|14	2	1					(US20260017435)\|Number of Claims: NCL=20\|Number of Drawings: NDR=14\|Number of Figures: NFG=14\|Independent Claim Number: ICL=1,14,19\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|	(US20260017435)\|Provisional Appl: US63/669,351 FDD=2024-07-10 [2024US-63669351]	(US20260017435)\|ENGLISH (ENG)	(US20260017435)\|Patent	Titre: (US20260017435)\|Technologies for modeling carbon dioxide removal Résumé: (US20260017435)\|Technologies for modeling carbon dioxide removal include a compute device with circuitry configured to obtain parameter data for use in modeling carbon dioxide removal from the atmosphere through enhanced rock weathering. The circuitry may also be configured to produce, using one or more models from a library of models, at least one prediction indicative of an amount of carbon dioxide that will be removed through enhanced rock weathering, including simulating co-precipitation of iron with one or more toxic metals. Further, the circuitry may be configured to present a visual representation of the at least one prediction in a user interface. Other embodiments are also described and claimed.	1	Abstract	gpt-4o-mini	yes	The article discusses enhanced rock weathering as a method for carbon dioxide removal, which aligns with the topic of accelerated weathering of rocks for CO₂ capture.
4	US63/601,059P\|US18/954,208	US18/954,208	US20250164404	114579754	US20250164404 A1 2025-05-22 [US20250164404]	2023-11-20\|2024-11-20	2024-11-20	2025-05-22		(US20250164404)\|2044-11-20	(US20250164404)\|System and method for enhanced rock weathering monitoring, reporting, and verification	(US20250164404)\|A method and system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. In some embodiments, the method includes emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area. The method includes determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target. The method includes converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target. The method also includes analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools. The method further includes providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.	IMPOSSIBLE SENSING\|MATI CARBON PBC	(US20250164404)\|Impossible Sensing LLC ([US])\|Mati Carbon PBC ([US])	SOBRON PABLO\|JORDAN JACOB S\|AGARWAL SHANTANU	(US20250164404)\|Sobron Pablo\|Jordan Jacob S.\|Agarwal Shantanu		(US20250164404)\|By measuring the SOC level, the present disclosure facilitates the correlation between changes in organic carbon attributable to rock dust application, thereby offering valuable insights into soil improvement.\|The present system allows improved statistical accuracy with pooled/composite soil samples, as shown in 402.\|This dual system enables the simultaneous determination of organic carbon and elemental composition in samples. This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status.\|However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions.\|However, understanding the ecosystematic changes in soils is complex, as conditions may vary across a single plot of land.\|MRV is technically difficult due to the long timescales and uncertainties associated with the chemical and physical processes involved.\|	(US20250164404)\|1. A system for monitoring, reporting, and verification of enhanced rock weathering comprising: a spectroscopy device comprising an optical source and a detector, wherein the optical source is configured to emit one or more optical signals directed to a target collected from a target area, and the detector is configured to determine spectral measurements of the optical signals collected from the target; and a data analysis subsystem coupled to the spectroscopy device and configured to: convert the spectral measurements to data indicating compositional characteristics of the target; analyze the data indicating compositional characteristics of the target using a plurality of analytical tools; and provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\|14. A method for monitoring, reporting, and verification of enhanced rock weathering comprising: emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area; determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target; and converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target; analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools; and providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.\|	(US20250164404)\|In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for calculating heavy metal concentrations 308, e.g., the amounts of metallic elements (often toxic) found in the soils or rock dust used for ERW.\|In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating specific soil elements 306, for example, the nitrogen (N), phosphorus (P), and potassium (K) content of the soil.\|In some embodiments, the present disclosure describes a LIBS device (e.g., 204) used for determining weathering status 304.\|	(US20250164404)\|ENHANCED ROCK(100,22)\|REPORTING(100,13)\|MONITORING(100,11)\|VERIFICATION(100,7)\|ENHANCED ROCK VERIFICATION(100,4)\|SPECTRAL MEASUREMENT(90,13)\|SPECTROSCOPY(69,19)\|ANALYTICAL INSTRUMENT(59,9)\|WEATHERING STATUS(56,9)\|DRY LAND EVALUATION(55,1)\|ENHANCED ROCK WEATHERING VERIFICATION(51,2)\|SOIL COMPLEXITY(51,1)\|ASSESSMENT(48,10)\|DATA ANALYSIS SUBSYSTEM(47,25)\|WEATHERING PREDICTION(45,6)\|INSIGHT(41,13)\|IDENTIFYING GEOLOCATED ZONE(41,1)\|STATISTICAL ACCURACY(40,1)\|EMPIRICAL MODEL(38,7)\|MULTIVARIATE DISTRIBUTION MODEL(36,6)\|VALUABLE INSIGHT(36,3)\|POOLED SAMPLE(33,12)\|ECOSYSTEMATIC CHANGE(32,1)\|HEAVY CATION(29,2)\|CATION COVARIANCE ANALYSIS(28,6)\|ROCK LOSS(27,3)\|SIGNAL TRANSMITTER(26,2)\|LONG TIMESCALE(26,1)\|EARTH AUGER(25,5)\|CARBON CREDIT CREATION(24,6)\|ENHANCED WEATHERING POTENTIAL(23,7)\|CARBON DIOXIDE REMOVAL(22,31)\|LAND SINGLE PLOT(22,1)\|UNCERTAINTY(21,2)\|DATA ANALYSIS(20,29)\|SOILS(20,8)\|CARBON DIOXIDE(19,36)\|CORRELATION(19,2)\|LIGHT CATION(19,2)\|LASER INDUCED BREAKDOWN SPECTROSCOPY(18,132)\|ENHANCED ROCK WEATHERING(17,41)\|TARGET AREA(16,26)\|ORGANIC CARBON(16,3)\|SOIL IMPROVEMENT(16,1)\|BIOAVAILABLE NUTRIENT QUANTIFICATION(15,1)\|SINGLE PLOT(15,1)\|MRV(14,16)\|CALCULATING HEAVY METAL(14,2)\|PATCHWORK SMALLHOLDER FARM(14,1)\|SOIL SAMPLE(13,11)\|CALIBRATION CURVE(13,10)\|INFIELD DEPLOYMENT(13,3)\|COVARIANCE COMPREHENSIVE ASSESSMENT(13,1)\|INTERSAMPLE HETEROGENEITY COMPREHENSIVE EXAMINATION(13,1)\|PELLETIZED SUBSAMPLE RASTERED ANALYSIS(13,1)\|HEAVY METAL(12,10)\|ROCK(11,5)\|IGNITION(11,3)\|SOIL HETEROGENEITY(11,3)\|COMPOSITIONAL CHARACTERIZATION(11,2)\|ECONOMICALLY DISADVANTAGED COMMUNITY(11,1)\|PHOSPHORUS P(11,1)\|OCEAN ACIDIFICATION(10,2)\|PREDICTION MODEL(10,2)\|INCENTIVIZE EMISSION AVOIDANCE(10,1)\|OCEAN FLORA HEALTH(10,1)\|ROBUST MRV FRAMEWORK(10,1)\|TOTAL CARBON DIOXIDE(9,6)\|AUTOFOCUSING COMPONENT(9,5)\|OPTICAL SOURCE(9,5)\|AGRICULTURAL SETTING(9,4)\|DEPTH INTEGRATED SOIL PROFILE(9,4)\|INDUCTIVELY COUPLED PLASMA(9,4)\|AQUEOUS METAL(9,3)\|CARBON CREDIT GENERATION CREDIBILITY(9,3)\|MANAGING STATE(9,3)\|GEOLOCATED ZONE SOIL SAMPLING(9,1)\|GRADUAL ROCK DISSOLUTION(9,1)\|ROCK WEATHERING STATUS(9,1)\|CARBON CAPTURE(8,8)\|ORGANIC CARBON MEASUREMENT(8,3)\|AGRONOMIC COBENEFIT(8,1)\|BASALT DISSOLUTION(8,1)\|CORAL ECOSYSTEM(8,1)\|DISHONEST ACTOR(8,1)\|DOMINANT SPECIATION(8,1)\|ENHANCE OCEAN ALKALINITY(8,1)\|GEOLOCATED ZONE SAMPLING(8,1)\|GROUNDWATER RUNOFF(8,1)\|INVALUABLE INSIGHT(8,1)\|NUTRIENT REQUIREMENT ESTIMATION(8,1)\|PREDICTING WEATHERING(8,1)\|PULVERIZED ROCK DUST(8,1)\|ROCK MINERAL BREAKDOWN(8,1)\|SOIL PENETRATION(8,1)\|TRADABLE CERTIFICATE(8,1)\|ALKALI SILICATE MINERAL(7,3)\|EMPIRICALLY DRIVEN MODEL(7,3)\|LIGHT COLLECTION OPTICS(7,3)\|AGRICULTURAL LAND(7,2)\|GRAPHICAL REPRESENTATION(7,2)\|AGRICULTURAL SOILS(7,1)\|BICARBONATE PRECIPITATION(7,1)\|BROAD ELEMENTAL COVERAGE(7,1)\|CENTRAL COMPOSITIONAL TENDENCY ASSESSMENT(7,1)\|COLLABORATIVE FRAMEWORK(7,1)\|FLUORESCENCE SPECTRUM(7,1)\|FORESTRY INTERVENTION(7,1)\|GEOLOGICAL ATTRIBUTE(7,1)\|ICP MS CALIBRATION INTEGRATION(7,1)\|RELIABLE CALIBRATION FRAMEWORK(7,1)\|ROBUST CALIBRATION(7,1)\|ROOT RESPIRATION(7,1)\|SOIL SUITABILITY(7,1)\|SPATIAL HETEROGENEITY GRANULAR UNDERSTANDING(7,1)\|STANDARDIZED REPORTING(7,1)\|SYSTEMATIC VARIABILITY(7,1)\|TANGIBLE NONVOLATILE PROGRAM CARRIER(7,1)\|UNLISTED ITEM(7,1)\|WEATHERING OUTCOME(7,1)\|ANALYSIS COMPONENT(6,8)\|GENERATING CARBON CREDIT(6,4)\|DEPTH INTERVAL(6,2)\|ELEMENTAL COMPOSITION ANALYSIS(6,2)\|KEY CATION(6,2)\|MOTOR INSTRUMENT(6,2)\|QUANTITATIVE ELEMENTAL ANALYSIS(6,2)\|RASTER PATTERN(6,2)\|SEED MATTER(6,2)\|SOIL COLUMN(6,2)\|SUBCOMBINATION(6,2)\|SUPPORTING DATA(6,2)\|ACIDIC SOIL REMEDIATION(6,1)\|ADDRESS CHALLENGING(6,1)\|AGRONOMIC BENEFIT(6,1)\|BUYER CONCERN(6,1)\|CARBON SEQUESTRATION KNOWABILITY(6,1)\|CRUCIAL INSIGHT(6,1)\|CRUCIAL ISSUE(6,1)\|DECISION INFORMATION(6,1)\|DEEP AQUIFER(6,1)\|DISSOLVE BICARBONATE(6,1)\|ELEMENTAL IDENTIFICATION(6,1)\|FARMER BURDEN(6,1)\|INTEGRATING UNCERTAINTY MODELING(6,1)\|MARKUP LANGUAGE(6,1)\|MEASUREMENT MISFIT(6,1)\|MINERAL CLASSIFICATION(6,1)\|MOBIL INSTRUMENT(6,1)\|MULTITHREADED PROCESSOR(6,1)\|PELLETIZING SOIL(6,1)\|POOLED SAMPLE UTILIZATION(6,1)\|PRESSED PELLETIZED SUBSAMPLE(6,1)\|REPLANT TREE(6,1)\|ROCK DUST ARRAY(6,1)\|SCRIPT INSTRUCTION(6,1)\|SOIL FERTILITY ASSESSMENT(6,1)\|SOIL SPATIAL VARIABILITY(6,1)\|SUBSURFACE NEAR CROP(6,1)\|UNTREATED SEWAGE SLUDGE(6,1)\|VERSATILE SAMPLING(6,1)\|SOIL ORGANIC CARBON(5,10)\|HCO(5,6)\|MRV(5,6)\|METAL(5,5)\|DECISION MAKING INFORMATION(5,3)\|FERTILIZER(5,3)\|MEASURING CARBON(5,3)\|SEA(5,3)\|TARGET SAMPLE(5,3)\|SAMPLE PROBE(5,2)\|3G WIRELESS MODEM(5,1)\|4G WIRELESS MODEM(5,1)\|ABSENT INCLUSION(5,1)\|ALKALINE MINERAL(5,1)\|ANALYTICAL ACCURACY(5,1)\|BASALT WEATHERING REACTION(5,1)\|BICARBONATE DRAW(5,1)\|COMPOSITIONAL ANALYSIS(5,1)\|COORDINATED FILE(5,1)\|COVARIANCE RELATIONSHIP(5,1)\|DEMAND FULFILLMENT(5,1)\|DEPTH PROFILING(5,1)\|DETECTING CARBON DECEPTION(5,1)\|DISSOLVED CARBON DOMINANT(5,1)\|ECOLOGICAL RISK(5,1)\|EXCLUSIVITY TERM(5,1)\|FUTURE OBSTACLE(5,1)\|GRID ANALYSIS(5,1)\|INFIELD ANALYSIS(5,1)\|INSTRUCTION INTERPRETATION(5,1)\|LASER IRRADIATION(5,1)\|MINERAL BICARBONATE(5,1)\|MODELING UNCERTAINTY(5,1)\|MRV QUALITY(5,1)\|NONNORMAL DISTRIBUTION(5,1)\|PH AMENDMENT(5,1)\|PHYSICAL(5,1)\|PLASMA PLUME(5,1)\|POOLED SAMPLE ACCURATE MEASUREMENT(5,1)\|PRECISE CHARACTERIZATION(5,1)\|PROCESSOR FIRMWARE(5,1)\|QUANTIFICATION ANALYSIS(5,1)\|RAW ROCK SAMPLE(5,1)\|REPORT CARBON SEQUESTRATION(5,1)\|ROBUST ANALYSIS(5,1)\|ROBUST MONITORING(5,1)\|SAMPLE HANDING(5,1)\|SATELLITE SENSOR(5,1)\|SERVER DISTRIBUTION(5,1)\|SOIL QUALITY PRECISE ASSESSMENT(5,1)\|SOILS TRANSITION(5,1)\|SPECTROSCOPY MEASUREMENT(5,1)\|TARGET VARIANCE(5,1)\|VERIFIABLE CARBON CREDIT(5,1)\|WORKFLOW PROPOSITION(5,1)\|CARBON DISSOLUTION(4,2)\|CENTRALIZED COMPUTING(4,2)\|GRAVEL(4,2)\|MULTITASKING(4,2)\|OPTIMIZATION(4,2)\|TRACTOR(4,2)\|ADJUSTING ROCK(4,1)\|AGGREGATING SOIL SAMPLE(4,1)\|ALKALINE SILICATE MINERAL POTENTIAL(4,1)\|BASELINE INFORMATION(4,1)\|CALCIUM CARBONATE MINERAL(4,1)\|CALCULATION REPRESENTATION(4,1)\|CARBON BEHAVIOR(4,1)\|CARBON CREDIT GENERATION RELIABILITY(4,1)\|CARBON CREDIT SALE(4,1)\|CARBON DIOXIDE SEQUESTRATION POTENTIAL(4,1)\|CARBON MEASUREMENT ISSUE(4,1)\|CARBON STORAGE PERMANENCE(4,1)\|CARBON UPTAKE(4,1)\|CLOUD PROCESSING(4,1)\|CLOUD STORAGE(4,1)\|COMPUTING ENVIRONMENT(4,1)\|DEEP UNDERSTANDING(4,1)\|EMBODIED COMPUTER SOFTWARE(4,1)\|ENHANCING MEASURE(4,1)\|ENSURING STABILITY(4,1)\|EXECUTION ENVIRONMENT(4,1)\|FLASH MEMORY(4,1)\|FOSSIL FUEL COMPANY(4,1)\|GEOLOGICAL TIMESCALE(4,1)\|INITIATIVE(4,1)\|INORGANIC CARBON AQUEOUS SPECIES(4,1)\|INSTANTIATION(4,1)\|MAJOR AQUEOUS SPECIES(4,1)\|MICROHETEROGENEITY(4,1)\|MIDDLEWARE COMPONENT(4,1)\|MOBILE VEHICLE(4,1)\|NET EMISSION(4,1)\|ORDINAL TERM(4,1)\|ORDINARY MEANING(4,1)\|PH RISE(4,1)\|PHYTOREMEDIATION(4,1)\|POOLED SOIL SAMPLE(4,1)\|POOLING SAMPLE(4,1)\|PRIMARY FACET(4,1)\|QUANTIFYING CARBON CREDIT(4,1)\|QUICK ADJUSTMENT(4,1)\|ROBOTIC ARM(4,1)\|ROCK POWDER(4,1)\|SAMPLE PRESENTATION(4,1)\|SOIL QUALITY ASSESSMENT(4,1)\|SOIL SAMPLING TECHNIQUE ADVANCE(4,1)\|SPECIES DISTRIBUTION(4,1)\|STANDARDIZED SUBSTRATE(4,1)\|TRUSTWORTHINESS(4,1)\|VARIABLE FOCUS LENS(4,1)\|WIRELESS INTERFACE(4,1)\|MACHINE LEARNING(3,3)\|SOIL SAMPLE COLLECTION(3,3)\|STRATEGY(3,3)\|WEB BROWSER(3,3)\|STRUCTURED GRID(3,2)\|ACCOUNTABILITY(3,1)\|AGNOSTIC(3,1)\|AGRICULTURAL MACHINERY(3,1)\|ANALYSIS REPRESENTATION(3,1)\|APPLYING CRUSHED ROCK PRACTICE(3,1)\|ARTIFICIALLY GENERATED PROPAGATED SIGNAL(3,1)\|ATMOSPHERIC CARBON DIOXIDE(3,1)\|AUDITORY FEEDBACK(3,1)\|BASELINE DATA(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON GAIN(3,1)\|CENTURY(3,1)\|CHANGING GROUND(3,1)\|CLIENT SERVER RELATIONSHIP(3,1)\|COLLECTED LIGHT PULSE(3,1)\|COMPARABILITY(3,1)\|COMPOSITIONAL ARRAY RANGE(3,1)\|COMPUTER PROGRAM INSTRUCTION(3,1)\|CONSERVATION(3,1)\|CREATING CARBON CREDIT(3,1)\|DEDUCE(3,1)\|DISCRETE REGION(3,1)\|DISPLAYING INFORMATION(3,1)\|DRONE(3,1)\|DUST SAMPLE(3,1)\|EMISSION TEST(3,1)\|ENHANCED WEATHERING PRACTICE(3,1)\|ENVIRONMENTAL ASSESSMENT(3,1)\|EQUIVALENT STRUCTURE(3,1)\|EXPRESS SUPPORT(3,1)\|FACTORING(3,1)\|FITTING MULTIVARIATE NORMAL(3,1)\|GAME CONSOLE(3,1)\|	(US20250164404)\|What is claimed is:\|1. A system for monitoring, reporting, and verification of enhanced rock weathering comprising:\| a spectroscopy device comprising an optical source and a detector, wherein the optical source is configured to emit one or more optical signals directed to a target collected from a target area, and the detector is configured to determine spectral measurements of the optical signals collected from the target; and\| a data analysis subsystem coupled to the spectroscopy device and configured to:\| convert the spectral measurements to data indicating compositional characteristics of the target;\| analyze the data indicating compositional characteristics of the target using a plurality of analytical tools; and\| provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\|2. The system of claim 1, wherein, to convert the spectral measurements to the data indicating compositional characteristics of the target, the data analysis subsystem is further configured to determine a weathering status, evaluate target contents, calculate heavy metal concentration, determine metal ratios in the target, or measure organic carbon in the target.\|3. The system of claim 2, wherein, to determine the weathering status, the data analysis subsystem is further configured to determine loss of rock dust by assessing composition of cations in rock dust applied to the target area through the enhanced rock weathering.\|4. The system of claim 2, wherein the heavy metal concentration is calculated in response to receiving bio-availability of metals and dissolved aqueous metals.\|5. The system of claim 2, wherein the soil organic carbon is measured based on determining loss of material on ignition.\|6. The system of claim 1, wherein the target is a pooled sample that includes soil samples collected and combined from multiple locations within the target area.\|7. The system of claim 6, further comprising a sampling handing unit configured to identify geolocated zones within the target area from which the pooled sample is collected, wherein the pooled sample is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling.\|8. The system of claim 1, wherein, to analyze the data indicating compositional characteristics, the data analysis subsystem is further configured to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS.\|9. The system of claim 1, wherein, to provide the assessments on carbon dioxide removal and insights on enhanced rock weathering, the data analysis subsystem is further configured to create a prediction model to provide data support for subsequent implementation of enhanced rock weathering.\|10. The system of claim 1, wherein, to provide the assessments on carbon dioxide removal and insights on enhanced rock weathering, the data analysis subsystem is further configured to determine one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.\|11. The system of claim 1, wherein the spectroscopy device is a handheld LIBS device.\|12. The system of claim 1, wherein the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and wherein the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis.\|13. The system of claim 1, wherein the spectroscopy device is a LIBS device that is combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic from the target.\|14. A method for monitoring, reporting, and verification of enhanced rock weathering comprising:\| emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area;\| determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target; and\| converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target;\| analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools; and\| providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.\|15. The method of claim 14, wherein converting the spectral measurements comprises one or more of determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target.\|16. The method of claim 15, wherein determining the weathering status comprises determining loss of rock dust by assessing composition of cations in rock dust applied to the target area through the enhanced rock weathering.\|17. The method of claim 14, further comprising identifying geolocated zones within the target area from which the target is collected, wherein the target is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling.\|18. The method of claim 14, wherein analyzing the data indicating compositional characteristics comprises performing one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS.\|19. The method of claim 14, wherein providing the assessments on carbon dioxide removal and insights on enhanced rock weathering comprises determining one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.\|20. The method of claim 14, wherein the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and wherein the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis.	(US20250164404)\|CROSS REFERENCE TO RELATED APPLICATION\|[0001] This application claims the benefit of U.S. Provisional Patent Application No. 63/601,059, titled “System and Method for Enhanced Rock Weathering Monitoring, Reporting, and Verification,” and filed on Nov. 20, 2023, the entire content of which is incorporated by reference herein.\|(US20250164404)\|TECHNICAL FIELD\|[0002] This disclosure relates to compositional characterization techniques, in particular, to optical devices that embody new methodologies for monitoring, reporting, and verification (MRV) of enhanced rock weathering (ERW).\|BACKGROUND\|[0003] Enhanced rock weathering (ERW) is the practice of applying crushed rocks and silicate minerals to agricultural land. It is a promising scalable and cost-effective carbon dioxide removal (CDR) strategy with significant environmental and agronomic co-benefits. However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions. Most current projects/systems/devices cannot accurately obtain carbon measurement and properly report carbon sequestration. Also, ERW lacks a robust monitoring, reporting, and verification (MRV) framework to address challenging problems such as carbon deception. For example, current MRV practices cannot provide a framework to easily detect and process a fraudulent claim of carbon gains by dishonest actors in the system.\|SUMMARY\|[0004] To address the aforementioned shortcomings, a method and a system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. The method include using a spectroscopy device to emit one or more optical signals directed to a target collected from a target area and to determine spectral measurements of the optical signals collected from the target. The method also includes using a data analysis subsystem to convert the spectral measurements to data indicating compositional characteristics of the target, analyze the data indicating compositional characteristics of the target using a plurality of analytical tools, and provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\|[0005] To convert the spectral measurements to the data indicating compositional characteristics of the target, one or more of the processes, such as determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. To determine the weathering status, loss of rock dust is determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering. To analyze the data indicating compositional characteristics, analytical tools are used to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS. To provide the assessment on carbon dioxide removal and insights on enhanced rock weathering, a prediction model is created to provide data support for subsequent implementation of enhanced rock weathering, and/or one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential are determined.\|[0006] In some embodiments, the heavy metal concentration is calculated in response to receiving bio-availability of metals and dissolved aqueous metals. In some embodiments, the soil organic carbon is measured based on determining the loss of material on ignition. In some embodiments, the target is a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling. In some embodiments, the spectroscopy device is a handheld LIBS device. In some embodiments, the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis. In some embodiments, the spectroscopy device is a LIBS device that is combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic from the target.\|[0007] The above and other preferred features, including various novel details of implementation and combination of elements, will now be more particularly described with reference to the accompanying drawings and pointed out in the claims. It will be understood that the particular methods and apparatuses are shown by way of illustration only and not as limitations. As will be understood by those skilled in the art, the principles and features explained herein may be employed in various and numerous embodiments.\|(US20250164404)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0008] The disclosed embodiments have advantages and features which will be more readily apparent from the detailed description, the appended claims, and the accompanying figures (or drawings). A brief introduction of the figures is below.\|[0009] FIG. 1A illustrates a block diagram of an exemplary ERW process.\|[0010] FIG. 1B illustrates a graphic representation of the speciation of a dominant form of dissolved carbon.\|[0011] FIG. 2A illustrates an overview of an exemplary laser induced breakdown spectroscopy (LIBS)-based data system, according to some embodiments.\|[0012] FIG. 2B illustrates an overall diagram of an exemplary LIBS device, according to some embodiments.\|[0013] FIG. 3 illustrates a block diagram of exemplary uses of LIBS devices in an MRV process for ERW, according to some embodiments.\|[0014] FIG. 4 illustrates a block diagram of exemplary features of LIBS devices and analysis used in MRV for ERW described in the present system, according to some embodiments.\|[0015] FIG. 5 illustrates a block diagram of exemplary data analysis and modeling used in the present system, according to some embodiments.\|[0016] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments.\|[0017] FIG. 7 illustrates a block diagram of an example computer system that may be used in implementing the technology described herein, according to some embodiments.\|(US20250164404)\|DETAILED DESCRIPTION\|[0018] The Figures (FIGs.) and the following description relate to preferred embodiments by way of illustration only. It should be noted that from the following discussion, alternative embodiments of the structures and methods disclosed herein will be readily recognized as viable alternatives that may be employed without departing from the principles of what is claimed.\|[0019] Reference will now be made in detail to several embodiments, examples of which are illustrated in the accompanying figures. It is noted that wherever practicable similar or like reference numbers may be used in the figures and may indicate similar or like functionality. The figures depict embodiments of the disclosed system (or method) for purposes of illustration only. One skilled in the art will readily recognize from the following description that alternative embodiments of the structures and methods illustrated herein may be employed without departing from the principles described herein.\|Scientific Introduction\|ERWA—A Durable Carbon Dioxide Removal Strategy\|[0020] Enhanced rock weathering (ERW) is a carbon dioxide removal (CDR) technique where naturally occurring mineral weathering reactions that consume atmospheric CO2 are accelerated. This may be achieved by applying crushed rocks and silicate minerals to agricultural soils. When the gradual rock dissolution or “weathering” occurs, alkaline minerals containing cations, such as calcium and magnesium (Ca2+ and Mg2+) that comprise the silicates, act as a pH amendment to remediate acidic soil on farms. In addition to balancing the pH of the soil, ERW can remove carbon dioxide from the atmosphere and sequester carbon for geological timescales.\|[0021] Basalt can be applied to managed land or an agricultural setting (e.g., rice paddies, corn fields, pasture lands) to practice ERW as a CDR strategy at scale. It should be recognized that the approach described herein is crop agnostic and can be generally applicable to any agricultural or managed land. As the dissolution of basalt proceeds, CO2 gas in the soil is converted to dissolved bicarbonate (HCO3−) in groundwater. This occurs due to basalt weathering reactions involving carbonic acid. Carbonic acid (H2O+CO2═H2CO3) is formed naturally in soils by plant respiration. The conversion of dissolved carbonic acid sources to bicarbonate draws CO2 down from the atmosphere.\|[0022] FIG. 1A illustrates a block diagram 100 of an exemplary ERW process. Basalt and/or other silicate materials (e.g., crushed rocks or “rock powder”) are applied to the soil and mixed into the subsurface near crops in 102. As the ERW progresses, the carbon dioxide (CO2 gas) from the respiration of roots 104 is converted to bicarbonate (HCO3−) in groundwater, and the CO2 stored in the soil 104 is also leached out of the soil and converted to bicarbonate. The bicarbonate is associated with a rising pH value of soil since the soil becomes less acidic. In this way, CO2 is removed. The silicate material application and CO2 isolation are associated with the deposition and sequestration processes 106, which results in the formation of weathering products in surface and groundwater runoff 108. Multiple enhanced rock weathering experiments have also demonstrated significant agronomic benefits due to improved nutrient supply for crops. Therefore, ERW deployments could aid farmers in regions where fertilizers are scarcely available or unaffordable.\|Carbon in Agricultural Setting\|[0023] The behavior of carbon in agricultural settings depends on the pH values in the settings. FIG. 1B illustrates a graphic representation 150 of the speciation of a dominant form of dissolved carbon, specifically, a representative calculation for the speciation of dissolved inorganic carbon (DIC). DIC is the sum of the aqueous species of inorganic carbon in a solution, which includes three major aqueous species: CO2, HCO3−, and CO32−. The speciation of DIC is the distribution of these species in a solution. The speciation of DIC can be determined by measuring the pH and total alkalinity of a solution and then using the measured values to calculate the concentrations of the different DIC species.\|[0024] To obtain the calculation demonstrating how the behavior of DIC changes with the pH value of soil in FIG. 1B, the pH value of the soil and pore waters of rice paddies is shifted towards pH=7 from ERW. As low pH (i.e., acidic) soils transition to neutral pH (i.e., pH≈7 ), dissolved CO2 is converted to the alkaline dissolved mineral bicarbonate (HCO3−). Near PH=7 bicarbonate is the dominant form of DIC. In other words, based on the shifting of the pH value, CO2 is converted to HCO3− and is not released as gas into the atmosphere.\|[0025] Next it is investigated what happens after CO2 is converted to other forms of dissolved inorganic carbon. After the conversion from CO2 to HCO3−, the bicarbonate (HCO3−) percolates into streams and rivers, from where the bicarbonate is delivered to the oceans. This DIC may reside in groundwater within the soil column for decades to centuries. This is an effective removal of carbon dioxide available to the ocean-atmosphere system. The eventual precipitation of bicarbonate as calcium carbonate minerals in deep aquifers or after transport to the ocean stably stores carbon for more than 10,000 years. The delivery of DIC to the ocean in the form of bicarbonate acts to enhance ocean alkalinity, which is vital for the health of ocean flora and fauna. For example, coral ecosystems have been particularly damaged by ocean acidification which is a well-known side effect of climate change. Ocean alkalinity enhancement works to counteract ocean acidification, as shown in 110 of FIG. 1A.\|Technical Problems\|[0026] It is hard to measure carbon capture. In agricultural and forest environments, many methods have been developed for measuring how much carbon is stored in soil. These methods significantly rely on labor-intensive mass-spectrometer measurements, spectroscopy, satellite-based sensors, and modeling. However, understanding the ecosystematic changes in soils is complex, as conditions may vary across a single plot of land. These methods cannot accurately evaluate carbon captured and retained in soils. Most current projects/methods cannot successfully quantify the amount of carbon, much less report carbon sequestration and conservation confidently. These schemes do not help address or incentivize emission avoidance and reduction by high-carbon industries (including agriculture).\|[0027] Even if the issue of carbon measurement can be solved, there are other challenges such as carbon deception. This is another main challenge related to the “net zero” demand in ecosystems. “Net zero” refers to a situation where an amount of carbon dioxide is removed from the atmosphere after that amount of carbon dioxide emission is generated, resulting in zero increase in net emissions. Thus, gas emission is still generated from human activity (e.g., fossil fuel companies can continue to explore, drill, extract, and burn fossil fuels), but carbon dioxide is taken out of the atmosphere in certain ways in some other places to balance out emissions. However dishonest actors may present during this procedure. For example, like a manufacturer rigging vehicles to cheat on emissions tests, forestry interventions may cut trees and then replant trees to claim carbon gains, i.e., carbon deception. Monitoring, reporting, and verification (MRV) is the process that can account for, communicate, and certify a CDR system's carbon removal over time. Currently, ERW lacks a robust MRV framework to obtain proper knowability of carbon sequestration (e.g., detecting carbon deception) and fill the knowledge gap to fulfill the demand of “net zero.”\|[0028] MRV is technically difficult due to the long timescales and uncertainties associated with the chemical and physical processes involved. Some crucial issues in MRV include accurately tracking carbon uptake, ensuring the permanence of carbon storage (e.g., long-time leakage risk), dealing with the variability of the process across different conditions, developing standardized reporting methods that ensure credibility and comparability across projects, etc. For example, there is no feasible way to directly measure the amount of CO2 removed from the atmosphere by ERW, and measuring CO2 in soils and groundwater is inherently challenging due to variability in environmental conditions (e.g., temperature, moisture levels, soil type, microbial activity). Emerging technologies (e.g., remote sensing, advanced soil sampling techniques) and research on effective MRV may help overcome some of the challenges.\|Overview\|[0029] The present disclosure proposes a novel system and method for performing compositional characterization of soil-rock dust mixtures. In some embodiments, the present system includes laser induced breakdown spectroscopy (LIBS) instruments that embody new MRV methodologies for ERW. LIBS deduces the elemental composition of a sample (e.g., solids, liquids, and gases) from measurements of the spectral line emission emitted by the plasma produced by high-power laser irradiation of the sample. LIBS will be described in further detail below.\|[0030] In some embodiments, the proposed workflow as described herein may include four primary facets:\| - i. Choose where to sample and measure compositional characteristics of soils;\| - ii. Determine how to measure compositional characteristics of the soils using LIBS;\| - iii. Analyze LIBS measurements (e.g., based on existing gold-standard measurement techniques); and\| - iv. Use post-processing analytical tools to create high-quality, verifiable carbon credits (a tradable certificate used to reduce global greenhouse gas emissions).\|[0035] The present disclosure also proposes multiple LIBS devices that may be employed in the field, workstations, or laboratories.\|[0036] FIG. 2A illustrates an overview of an exemplary LIBS-based data system 200 that is used to implement the functionalities described herein. In this example, system 200 includes a sample handling unit 202, a LIBS device 204, and a data processing unit 206. System 200 may use sample handling unit 202 to identify locations or zones that target samples (e.g., soil samples) should be collected from (e.g., geolocated zone-based soil sampling). Depending on different quantitative analyses and qualitative analyses to be performed (e.g., as described in FIGS. 3-6), sample handling unit 202 may also be used to instruct LIBS device 204 to obtain specific types of measurements. The present system may further use sample handling unit 202 to ensure the accurate positioning of a sample for optical interaction with LIBS device 204. LIBS device 204 is employed to obtain measurements and analysis data from samples, which will be described in detail in FIG. 2B. The data from LIBS device 204 is further analyzed and modeled by data processing unit 206 for the purpose of monitoring, reporting, and verification, for example, as illustrated in FIG. 5 below. Although only one LIBS device is shown in the example system 200 of FIG. 2A, it is possible that more LIBS devices and/or other units/components may be included in a LIBS-based data system.\|[0037] In some embodiments, at least a portion of the data processing unit 206 is part of a computer system (described below in FIG. 7) that is communicatively coupled to LIBS device 204. In other embodiments, at least a portion of the data processing unit 206 may be integrated into LIBS device 204. For example, data processing unit 206 may reside on a standalone computer system to perform advanced compositional analysis based on real-time sample analysis from data acquisition & analysis component 260 of LIBS device 204 (described below in FIG. 2B). Data processing unit 206 together with data acquisition & analysis component 260 form a data analysis subsystem that is responsible for various types of data processing, evaluation, calculation, etc, as described in the present disclosure. When LIBS device 204 is attached to or mounted on a motor instrument (e.g., vehicle, drone), the data analysis subsystem may be integrated into data acquisition onboard the motor instrument for real-time data acquisition and analysis. In some embodiments, at least a portion of the sample handling unit 202 may also be part of an external computer system and/or an integrated part of LIBS device 204. For example, sample handling unit 202 may be designed to use motorized stages or robots to move a sample in a controlled manner and thus is included in or attached to LIBS device 204 for precise sample positioning.\|LIBS Device\|[0038] LIBS is a rapid chemical analysis technology that uses a short laser pulse to create a micro-plasma on the sample surface. LIBS can be used to detect the presence of various elements in a sample based on directing a high-power emission from a laser onto the sample to form a plasma. The plasma is then analyzed spectroscopically to determine the composition of the sample. The LIBS is often used with a soil penetrating probe to detect heavy metal contamination in soil due to its high sensitivity and sample-free preparation. The LIBS analytical technique offers some other compelling advantages such as fast measurement time (e.g., a few seconds for a single spot analysis), broad elemental coverage (e.g., including, but not limited to, lighter elements such as H, Be, Li, C, N, O, Na, and Mg), versatile sampling protocols that include fast raster of the sample surface and depth profiling, etc.\|[0039] The present disclosure proposes new LIBS device(s) used in the MRV process for ERW. In some embodiments, the new LIBS device is a single multi-purpose optical device. In other embodiments, the new LIBS device may include one or more optical devices. Each device can be designed for a single purpose or multiple purposes. The LIBS devices may have various physical components and/or configurations.\|[0040] FIG. 2B illustrates an overall block diagram of an exemplary LIBS device 204, which includes some key components such as optical source 254, focusing and light collection optics 256, detector 258, and data acquisition & analysis component 260. These components are depicted merely for illustration, and other components (more or less) may be included in LIBS device 204. For example, sample probe 252 may be part of the LIBS device 204. In some embodiments, LIBS device 204 may use a sample probe 252 (e.g., a soil penetrating probe) to take a sample from a target area that is strategically identified (e.g., on managed land). In response, optical source 254 (e.g., a laser) may generate a high-energy light pulse that is directed onto the sample, and focusing and light collection optics 256 (e.g., lens, mirrors) may focus the light pulse to a specific point on the sample, thereby creating a plasma plume. The focusing and light collection optics 256 may also capture/collect the light pulse/beam to avoid light interference. The collected light pulse is then passed through detector 258 (e.g., spectrometer) to obtain sample measurements (e.g., spectral data). For example, detector 258 may disperse the light pulse into individual wavelengths, determine the intensity of light at each wavelength (e.g., using a charge-coupled device (CCD) or photo-multiplier tube (PMT)), and generate a spectrum that is characteristic of specific elements in the sample.\|[0041] Data acquisition & analysis component 260 may include computing hardware such as a central processing unit, memory, and storage, as described in the computer system of FIG. 7. Data acquisition & analysis component 260 is configured to receive the measurement data from detector 258 and perform the elemental composition analysis on the measurement data. In some embodiments, LIBS device 204 may also communicate with an alternative or additional data processing unit (e.g., 206) to perform LIBS analysis and any other elemental identification and quantification analyses. Based on the analysis, a result is generated in 262. For example, the result may be a report or graphical output showing the elemental composition of the sample. Various types of measurements and analyses may be conducted by the data analysis subsystem including data acquisition & analysis component 260 and data processing unit 206, which will be further described below with reference to FIGS. 3-6.\|[0042] The present system may deploy one or more improved LIBS devices to implement the disclosed functionalities. For example, the improved LIBS device (e.g., 204) may be equipped, attached, or associated with an autofocusing component to enable consistent, in-focus measurements of samples without moving other optical components. The autofocusing component may be included as a part of a suitable optical assembly that is hand-held, attached to a mobile vehicle, or integrated with a positioning system (e.g., robotic arm, boom, leg, conveyor belt), etc. Using the autofocusing component, spectroscopy measurements can be automatically focused based on a focal length of its optics relative to the target sample. Instead of using certain mechanisms (e.g., mechanical actuators) to change the position of the optical component(s), in some embodiments, the autofocusing component may include a shape changing lens (e.g., variable focus lens) to allow continuous tuning of a focal length and working distance of the autofocusing component relative to a target sample.\|Data Acquisition and Evaluation Using LIBS Device\|[0043] As discussed above, components 252, 254, 256, 258, and/or 260 of LIBS device 204 may work together with other units of data system 200 to acquire sample data and provide insights about the elemental composition of a sample (e.g., soil sample). In the illustrated embodiment of FIG. 3, one or more LIBS devices 204 may be used to determine weathering status 304, evaluate specific soil contents/elements 306, calculate heavy metal concentration 308, evaluate metal ratios in soils 310, and/or measure soil organic carbon 312. In some embodiments, one or more LIBS devices 200 may also be used to measure and analyze the compositional characteristics of soils, the biological composition of plant and seed matter, and the elemental composition of rock samples.\|[0044] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) used for determining weathering status 304. In some embodiments, a LIBS-based device may be employed to assess the composition of lighter cations relative to heavier cations in applied rock dust. This composition analysis may be used in determining the weathering status of the rock dust application on agricultural fields, pasture lands, or any other natural environments. Thus, an approach is obtained, for determining the loss of rock dust due to enhanced rock weathering (ERW) for the purpose of monitoring, reporting, and verification (MRV) to create carbon credits.\|[0045] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating specific soil elements 306, for example, the nitrogen (N), phosphorus (P), and potassium (K) content of the soil. This is the estimation of nutrient requirements, factoring in additional nutrients provided by rock dust application. The use of LIBS devices in elemental composition analysis can reduce farmers' burden to apply fertilizers (i.e., NPK nitrogen-phosphorus-potassium) while conducting ERW projects. LIBS allows the quantification of these additional bioavailable nutrients, which become active in the soil column with the breakdown of the rock minerals (e.g., being modified through chemical, physical, or biological interactions with rocks and minerals).\|[0046] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for calculating heavy metal concentrations 308, e.g., the amounts of metallic elements (often toxic) found in the soils or rock dust used for ERW. These elements may include metals such as lead (Pb), mercury (Hg), nickel (ni), etc., and can be found in pesticides, fertilizers, or untreated sewage sludge introduced into the soil. The heavy metal may accumulate in the environment to pose serious health and ecological risks. The disclosed LIBS device may provide insights into the safety considerations of cultivating various crops, for example, providing insights into phytoremediation such as using sunflowers to remove Strontium, which is poisonous metal to most other livings. According to US Environmental Protection Agency (EPA) standards, the bio-availability of metals and dissolved aqueous metals will be needed for calculating heavy metal concentrations.\|[0047] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating key metal ratios in soils for ERW 310. In some embodiments, critical metal ratios in soils are assessed using LIBS technology before the implementation of ERW (i.e., before the rock dust application for enhanced weathering). This process can be outlined as follows:\| - i. Sample Collection: soil samples are collected from the target area where ERW is planned. These samples represent the current soil composition in the region;\| - ii. LIBS Analysis: the collected soil samples are subjected to LIBS analysis. The LIBS device measures the elemental composition of the soil, providing baseline data on the concentrations of various metals being present;\| - iii. Trace metal ratios and potential pulverized rock dust field amendments may then be evaluated together to determine if the rock dust is appropriate for application to the field; and \| - a. Evaluate environmental concerns,\| - b. Evaluate the potential for signal strength in measurements: measuring key metal ratios for MRV process.\| - iv. Key Metal Ratios: specific metal ratios of interest, which are known to influence the effectiveness of ERW, are calculated based on the LIBS data. These key metal ratios often include ratios such as calcium to magnesium (Ca/Mg), calcium to potassium (Ca/K), or calcium to sodium (Ca/Na), among others.\|[0054] In some embodiments, the calculated key metal ratios are evaluated to determine the suitability of the soil for ERW. An ideal balance of these ratios is typically necessary for optimal carbon capture and weathering outcomes. The assessment results may guide decisions regarding the need for rock dust application and the specific rock dust type required to achieve the desired metal ratios for effective ERW.\|[0055] By employing LIBS technology for the evaluation of key metal ratios in soils before rock dust application for enhanced weathering, informed decision-making can be used to ensure that the chosen ERW strategy is tailored to the specific soil composition of the target area. This optimization may also contribute to efficient carbon dioxide removal and MRV.\|[0056] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for measuring soil organic carbon 312. A LIBS device can be used to measure soil organic carbon (SOC) levels. The SOC level represents the amount of carbon stored in the form of organic compounds in the soil, and SOC is critical to soil quality and carbon sequestration because it helps store carbon from the atmosphere and contributes to mitigating climate change. By measuring the SOC level, the present disclosure facilitates the correlation between changes in organic carbon attributable to rock dust application, thereby offering valuable insights into soil improvement. In some embodiments, soil organic carbon measurements may be approximated by the loss of material on ignition (LOI) (e.g., by measuring the weight loss of organic matter content after heating the sample to a high temperature).\|LIBS Analysis\|[0057] Numerous LIBS analyses may be conducted based on element measurements, calculation, and evaluation. In addition to in-depth soil analysis, when a LIBS device is used to measure the biological composition of plant and seed matter, the LIBS analysis can serve to validate the absence of potential metal accumulation resulting from enhanced weathering processes.\|[0058] In some embodiments, a LIBS device may also be used for rock sample analysis, where the elemental composition of raw rock samples from rock quarries or in the field is analyzed. This LIBS analysis may be applied to determine an enhanced weathering potential and a total carbon dioxide removal (CDR) potential. The enhanced weathering potential is the amount of atmospheric carbon dioxide that can be removed and stored through the ERW process (e.g., manual application of rocks or minerals) over a specific period of time. This factor may vary depending on the type of rocks/minerals used in ERW, the surface area available for reaction, environmental conditions (e.g., precipitation, temperature), etc. The total CDR potential is the amount of carbon dioxide that can be removed from the atmosphere in the long term, which depends on the effectiveness of the ERW process.\|[0059] In some embodiments, a spectral fluorescence device may be used in combination with LIBS analysis to create a dual system. This dual system enables the simultaneous determination of organic carbon and elemental composition in samples. This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status. In some embodiments, this approach may also be used to help refine soil organic carbon estimates outlined in 312 of FIG. 3. In general, the combination of LIBS and fluorescence may expand and strengthen the LIBS measurement and analysis, e.g., as discussed in FIG. 3.\|Beneficial Features of LIBS Device and Analysis\|[0060] FIG. 4 illustrates a block diagram 400 of exemplary features of LIBS devices and analysis used in the MRV process for ERW as described in the present system.\|[0061] The present system allows improved statistical accuracy with pooled/composite soil samples, as shown in 402. By aggregating soil samples from various locations within a field, the present system seeks to accurately determine the central compositional tendency and associated dispersion or variance in the soil's elemental composition. As compared to the current techniques, the utilization of pooled samples enables a more robust and representative analysis of the soil's overall composition, contributing to a more precise assessment of soil quality and environmental conditions. The accurate measurement of pooled samples is particularly important to soil fertility assessment, soil quality monitoring, and precision agriculture.\|[0062] The present system provides geolocated zone-based soil sampling for target characteristic assessment, as shown in 404. In some embodiments, the present system allows the collection of soil samples from specific geolocated zones within a field. By strategically pooling samples from these distinct zones, the analysis can yield precise data regarding the central tendency and variance of the target characteristic within each zone. This geolocated zone-based sampling approach offers a granular understanding of the spatial heterogeneity, distribution, and variability of the target characteristic, thereby enabling informed decision-making for soil management and ERW applications. Potential future obstacles with a MRV process based on soil heterogeneity may also be addressed by examining measurements at this juncture. In some embodiments, zones may be determined based on soil type, gridded areas, etc. A zone may also be small, predefined regions that include, but are not limited to, a circular region with a predefined radius or a square area with a predefined side length.\|[0063] The LIBS device of the present system can be used in rock sample analysis to determine enhanced weathering potential and total carbon dioxide removal (CDR) potential. In particular, the present system may evaluate the carbon dioxide potential of alkaline silicate minerals, as shown in 406. The present system can assess the carbon dioxide potential of alkaline silicate minerals including, but not limited to, basalt, olivine, and wollastonite. These minerals are known for their capacity to sequester carbon dioxide through enhanced weathering processes. In some embodiments, the present system may utilize a LIBS device to analyze the elemental composition of these minerals and determine their specific potential for CDR. By accurately quantifying the CDR potential of alkaline silicate minerals, the present system gains valuable insights into the efficacy of a CDR solution.\|[0064] The present system allows systematic preparation of pressed-pelletized subsamples derived from pooled soil samples, as shown in 408. By compressing and pelletizing soil material from each pooled sample, the present system may create a consistent and standardized substrate for LIBS analysis. This process can minimize variations in sample presentation, ensuring reliable and reproducible results during LIBS analysis. This process further streamlines the handling of samples, allowing for an efficient assessment of the central compositional tendency and variance of the target characteristics within the soil, and ultimately enhancing the accuracy of soil quality and environmental assessments.\|[0065] The present system further allows grid-based or rastered LIBS sampling for in-depth soil core analysis, as shown in 410. In some embodiments, the present system may conduct grid-based or rastered analyses of the pelletized subsamples, where the LIBS device systematically scans and analyzes discrete regions or points on the pellet surface in a structured grid or raster pattern. This approach enables a comprehensive examination of the intersample heterogeneity (or microheterogeneity) of soil characteristics and the distribution of elemental composition within the subsamples.\|[0066] Through this analysis, the present system may achieve a high-resolution understanding of the central compositional tendency and variance of the target characteristics in the soil, and the detailed information may provide invaluable insights into the spatial variability of soil properties, thereby enhancing precision in soil quality assessment and MRV for CDR applications.\|[0067] Using rasterized or gridded LIBS sampling can also systematically measure the elemental composition of intact soil cores at various depths. By taking measurements in a prescribed structured grid or raster pattern for LIBS analysis along the length of an intact soil core, the present approach enables precise characterization of the compositional variations with depth. This is particularly beneficial for understanding how soil properties change at different depths within the core, offering crucial insights into subsurface composition and environmental conditions. The present system seeks to assess soil heterogeneity and geological attributes with depth, contributing to informed decisions in ERW applications and MRV techniques.\|Device Characteristics and Deployment\|[0068] The present system supports specific device characteristics and deployment that are beneficial to the MRV process for ERW. In some embodiments, the present system supports handheld and miniaturized LIBS devices for soil sampling, field-based depth-integrated soil profiling with LIBS and soil auger, and in-field deployment of LIBS technology on motor vehicles, etc.\|[0069] The LIBS device described herein can be a handheld device that is portable, easy to operate, and suitable for rapid data acquisition. This handheld device is particularly useful in patchwork small-holder farms (e.g., rice paddies). It is engineered to provide a simplified user interface while maintaining the analytical accuracy and precision required for soil and environmental analysis. Any instantiation of the LIBS device may contain fewer optical sensors than the original, making the device more affordable and lighter. As a result, this LIBS device is adaptive for use in rural, remote, and economically disadvantaged communities. In addition, the miniaturized form of the device enables the present system to perform real-time, in-situ analyses, contributing to timelier and data-driven decision-making processes in agriculture, geology, and environmental science.\|[0070] The present system also allows a LIBS device to be combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic. A soil auger is employed to collect soil samples at various depths within the field. These samples are representative of the soil composition at specific depth intervals.\|[0071] After and/or during the auguring process, the present system performs LIBS analysis on the collected soil samples. A LIBS device can rapidly and accurately measure the elemental composition of the soil samples, including the concentration of the target characteristic of interest. The present system may then integrate the LIBS data obtained from each depth interval to construct a depth-integrated soil profile of the target characteristic. This profile provides a comprehensive understanding of how the target characteristic varies with depth within the soil.\|[0072] A LIBS device/instrument can be deployed in different ways. In some embodiments, the present system supports in-field deployment of LIBS technology on motor vehicles. LIBS is integrated into motor vehicles, such as tractors or other agricultural machinery, for in-field deployment. The present system seamlessly integrates LIBS instrumentation into the design of motor vehicles used for field operations, such as tractors.\|[0073] The LIBS device can be securely mounted, ensuring stability during vehicle movement. The LIBS device may operate in real time as the motor vehicle traverses the field. The LIBS device continuously analyzes the soil or other target materials as the vehicle moves, providing instant elemental composition data. The present system may collect LIBS-generated data and integrate the data into a data acquisition (DAQ) onboard the vehicle, allowing for real-time decision-making based on soil or material composition. A vehicle operator can use the LIBS data to make immediate adjustments to field operations for any ERW-related purpose, such as varying fertilizer application rates or adjusting rock dust application rates based on the in-field analysis. The present system may log the LIBS data, providing a detailed record of the soil or material composition across the field for subsequent analysis and optimization.\|[0074] In some embodiments, the present system may support other deployment methods. For example, one or more LIBS devices may be integrated into drones, underwater vehicles/amphibious, or other mobil instruments.\|Data Analysis and Modeling\|[0075] FIG. 5 illustrates a block diagram 500 of exemplary features of data analysis and modeling used in the present system. As depicted in FIG. 5, the data analysis and modeling 502 of the present system may be featured with various analytical tools such as multivariate distribution modeling for cation covariance analysis 504, empirical modeling for weathering prediction and carbon credit creation 506, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data 508, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS 510, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV 512. In some embodiments, these data analyses and modeling may be performed at least by data processing unit 206 in combination with data acquisition & analysis component 260 as shown in FIGS. 2A and 2B (i.e., data analysis subsystem).\|[0076] The present system provides multivariate distribution modeling for cation covariance analysis, as shown in 504. In some embodiments, the LIBS data can be leveraged for analyzing and modeling the covariance relationships among key cations in soil including, but not limited to, titanium, calcium, sodium, magnesium, potassium, phosphorous, and nitrogen. In some embodiments, the present system entails fitting multivariate normal or non-normal distributions to the data obtained through LIBS measurements.\|[0077] Multivariate distribution fitting allows for the comprehensive assessment of the covariance and correlations between key cations in soil. It provides valuable insights into the simultaneous variations and relationships among these elements, contributing to a deep understanding of soil composition and baseline information required for MRV. The present system uses LIBS to provide dense and rapid enough data to find systematic variances in soil heterogeneity within any given field, pasture, agricultural setting, or any other natural setting.\|[0078] In some embodiments, the present system may apply the quantitative elemental analysis approach as described in Sobron, titled “non-linear methods for quantitative elemental analysis and mineral classification using laser-induced breakdown spectroscopy (LIBS),” U.S. patent application Ser. No. 15/998,391, which is hereby incorporated by reference in its entirety.\|[0079] In some embodiments, the present system supports empirical modeling for weathering prediction and carbon credit creation, as shown in 406. That is, data collected in the present system can be leveraged to develop an empirically driven model for predicting the weathering of rock dust applied to fields and providing suggestions and instructions for subsequent ERW implementation.\|[0080] The empirical model may help the monitoring, reporting, and verification (MRV) process, which aims at quantifying the carbon capture potential resulting from enhanced weathering practices. By using dense, LIBS-generated data to create a predictive model, it becomes possible to monitor and report on the efficiency of carbon capture using regression-based and/or machine-learning methods. As a result, the time between data collection and sales for creating carbon credits may be reduced. The empirically driven model therefore facilitates accurate and data-driven MRV processes while incentivizing an easy switch to practices where carbon credits may be created through ERW. For example, when structure a predictive model, the present system may use mineral type, application rate, surface area of mineral, climate data, and environmental carbon dioxide concentration as input parameters of the model. The present system may calculate the weathering rate based on the environmental conditions and mineral properties, calculate the sequestration of carbon dioxide, and use weathering rate equations to predict how much carbon dioxide may be captured within a specific area over a specific timeframe. The present system may also calculate the total carbon dioxide removal rate to estimate global or regional carbon dioxide sequestration potential.\|[0081] To ensure accuracy and precision, in some embodiments, the present system may calibrate the LIBS device using high-precision measurements obtained from ICP-MS, as shown in 508.\|[0082] ICP-MS represents a well-established and highly accurate analytical technique, known for its exceptional precision in measuring elemental composition. By calibrating the LIBS device against ICP-MS data, the present system may establish a robust and reliable calibration framework. This calibration method may serve to validate and fine-tune the LIBS measurements, ensuring accuracy and traceability to a gold standard in elemental analysis.\|[0083] The integration of ICP-MS calibration in the present system enhances the trustworthiness and consistency of LIBS measurements, and the enhanced measurements may be suitable for a wide range of ERW applications for MRV. This calibration approach boosts the credibility of LIBS technology in scientific research and regulatory compliance (e.g., metals contamination according to EPA standards).\|[0084] The present system supports the construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, as shown in 510. In some embodiments, the present system may use known mixtures of soil and rock dust to create calibration curves. With a soil sample and rock dust sample that have already been characterized via ICP-MS or other analytical techniques, the present system can obtain known mixtures such that the rock dust comprises a known percentage of the weight of a newly created sample. By testing many mixed samples using LIBS with an array of rock dust ranging from 0 to 100% weight by mass, the present system can determine a series of calibration curves. These curves may fit the compositional characteristics of a particular soil type-rock dust combination. The present system may then store the data for soil type-rock dust combinations, creating a large database of possible LIBS spectral signals for a range of possible compositional arrays. With a sufficiently large database, the present system can apply one or more regression-based, machine-learning-based tools, and principal component analysis to select the most optimal calibration curve for new measurement(s).\|[0085] Here, the present system aims to strengthen the credibility of carbon credit generation. In some embodiments, the present system may use the misfit of measurements to known calibration curves to quantify measurement uncertainty, so that carbon credit sales effectively incorporate potential variations in carbon capture into pricing structures.\|[0086] In some embodiments, the present system supports collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV, as shown in 512. In other words, ICP-MS and LIBS are used collaboratively to spot-check and validate the empirically driven model developed for CDR MRV. This process ensures that the model accurately reflects the carbon capture and sequestration processes in real-world applications, enhancing the reliability of carbon credit generation. The present system may also use the same collaborative framework to generate uncertainty models when upscaling the sample area for MRV. To upscale the sample area for MRV, test plots are used to make projections for larger fields, and/or several fields are used to project CDR for a region, etc. By systematically assessing variations and uncertainties using ICP-MS and LIBS data, these models provide insights into the potential variability in carbon capture estimates as the sample area is expanded. This information is essential for accurately quantifying carbon credits and assuaging buyers' concerns about the quality of carbon credits. The information is also crucial to assess the quality of MRV.\|[0087] The present system aims to strengthen the credibility of carbon credit generation and improve informed decision-making in ERW-related land management. By integrating uncertainty modeling, the present system enhances its ability to account for variations in carbon capture and carbon dioxide removal potential and provides a comprehensive assessment of carbon dioxide removal efforts. The present system may enhance the credibility of carbon credit generation while providing transparency and accountability in environmental initiatives.\|Flowchart\|[0088] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments. Method 600 may be implemented using a LIBS-based data system 200, as shown in FIGS. 2A and 2B. A spectroscopy device (e.g., LIBS device 204) is used to obtain measurements from a target sample. At step 602, the spectroscopy device (e.g., using optical source 254) emits one or more optical signals directed to a target collected from a target area (e.g., managed field or other agricultural settings). At step 604, the spectroscopy device (e.g., using detector 258) determines spectral measurements of the optical signals collected from the target. The target can be a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified (e.g., by sample handing unit 202) from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered LIBS sampling.\|[0089] As shown in FIGS. 2A and 2B, a data analysis subsystem (e.g., including data processing unit 206 and data acquisition & analysis component 260) is communicatively coupled to the spectroscopy device (e.g., LIBS device 204). At step 606, the data analysis subsystem is configured to convert the spectral measurements to data indicating compositional characteristics of the target, which includes at least one or more of determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. For example, to determine the weathering status, loss of rock dust may be determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering.\|[0090] The data analysis subsystem is then configured to analyze the data indicating compositional characteristics of the target using a plurality of analytical tools at step 608, and provide assessment on carbon dioxide removal and insights on enhanced rock weathering at step 610. In some embodiments, to analyze the compositional data, the data analysis subsystem uses various analytical tools to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision ICP-MS data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS, etc. To provide the assessment, the data analysis subsystem may also calculate one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.\|Computer Implementation\|[0091] In some examples, some or all of the processing described above can be carried out on a personal computing device, on one or more centralized computing devices, or via cloud-based processing by one or more servers. Some types of processing can occur on one device and other types of processing can occur on another device. Some or all of the data described above can be stored on a personal computing device, in data storage hosted on one or more centralized computing devices, and/or via cloud-based storage. Some data can be stored in one location and other data can be stored in another location. In some examples, quantum computing can be used, and/or functional programming languages can be used. Electrical memory, such as flash-based memory, can be used.\|[0092] FIG. 7 is a block diagram of an example computer system 700 that may be used in implementing the technology described herein. General-purpose computers, network appliances, mobile devices, or other electronic systems may also include at least portions of the system 700. The system 700 includes a processor 710, a memory 720, a storage device 730, and an input/output device 740. Each of the components 710, 720, 730, and 740 may be interconnected, for example, using a system bus 750. The processor 710 is capable of processing instructions for execution within the system 700. In some implementations, the processor 710 is single-threaded. In some implementations, the processor 710 is a multi-threaded processor. The processor 710 is capable of processing instructions stored in the memory 720 or on the storage device 730.\|[0093] Memory 720 stores information within the system 700. In some implementations, the memory 720 is a non-transitory computer-readable medium. In some implementations, the memory 720 is a volatile memory unit. In some implementations, the memory 720 is a non-volatile memory unit.\|[0094] The storage device 730 is capable of providing mass storage for the system 700. In some implementations, the storage device 730 is a non-transitory computer-readable medium. In various implementations, the storage device 730 may include, for example, a hard disk device, an optical disk device, a solid-state drive, a flash drive, or some other large-capacity storage device. For example, the storage device may store long-term data (e.g., database data, file system data, etc.). The input/output device 740 provides input/output operations for the system 700. In some implementations, the input/output device 740 may include one or more network interface devices, e.g., an Ethernet card, a serial communication device, e.g., an RS-232 port, and/or a wireless interface device, e.g., an 802.11 card, a 3G wireless modem, or a 4G wireless modem. In some implementations, the input/output device may include driver devices configured to receive input data and send output data to other input/output devices, e.g., keyboard, printer, and display devices 760. In some examples, mobile computing devices, mobile communication devices, and other devices may be used.\|[0095] In some implementations, at least a portion of the approaches described above may be realized by instructions that upon execution cause one or more processing devices to carry out the processes and functions described above. Such instructions may include, for example, interpreted instructions such as script instructions, executable code, or other instructions stored in a non-transitory computer-readable medium. The storage device 730 may be implemented in a distributed way over a network, such as a server farm or a set of widely distributed servers, or may be implemented in a single computing device.\|[0096] Although an example processing system has been described in FIG. 7, embodiments of the subject matter, functional operations, and processes described in this specification can be implemented in other types of digital electronic circuitry, in tangibly embodied computer software or firmware, in computer hardware, including the structures disclosed in this specification and their structural equivalents, or in combinations of one or more of them. Embodiments of the subject matter described in this specification can be implemented as one or more computer programs, i.e., one or more modules of computer program instructions encoded on a tangible nonvolatile program carrier for execution by, or to control the operation of, data processing apparatus. Alternatively or in addition, the program instructions can be encoded on an artificially generated propagated signal, e.g., a machine-generated electrical, optical, or electromagnetic signal that is generated to encode information for transmission to a suitable receiver apparatus for execution by a data processing apparatus. The computer storage medium can be a machine-readable storage device, a machine-readable storage substrate, a random or serial access memory device, or a combination of one or more of them.\|[0097] The term “system” may encompass all kinds of apparatus, devices, and machines for processing data, including by way of example a programmable processor, a computer, or multiple processors or computers. A processing system may include special-purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit). A processing system may include, in addition to hardware, code that creates an execution environment for the computer program in question, e.g., code that constitutes processor firmware, a protocol stack, a database management system, an operating system, or a combination of one or more of them.\|[0098] A computer program (which may also be referred to or described as a program, software, a software application, a module, a software module, a script, or code) can be written in any form of programming language, including compiled or interpreted languages, or declarative or procedural languages, and it can be deployed in any form, including as a standalone program or as a module, component, subroutine, or other unit suitable for use in a computing environment. A computer program may, but need not, correspond to a file in a file system. A program can be stored in a portion of a file that holds other programs or data (e.g., one or more scripts stored in a markup language document), in a single file dedicated to the program in question, or in multiple coordinated files (e.g., files that store one or more modules, sub programs, or portions of code). A computer program can be deployed to be executed on one computer or on multiple computers that are located at one site or distributed across multiple sites and interconnected by a communication network.\|[0099] The processes and logic flows described in this specification can be performed by one or more programmable computers executing one or more computer programs to perform functions by operating on input data and generating output. The processes and logic flows can also be performed by, and apparatus can also be implemented as, special purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit).\|[0100] Computers suitable for the execution of a computer program can include, by way of example, general or special purpose microprocessors or both, or any other kind of central processing unit. Generally, a central processing unit will receive instructions and data from a read-only memory, a random access memory, or both. A computer generally includes a central processing unit for performing or executing instructions and one or more memory devices for storing instructions and data. Generally, a computer will also include, or be operatively coupled to receive data from or transfer data to, or both, one or more mass storage devices for storing data, e.g., magnetic, magneto-optical disks, or optical disks. However, a computer need not have such devices. Moreover, a computer can be embedded in another device, e.g., a mobile telephone, a personal digital assistant (PDA), a mobile audio or video player, a game console, a Global Positioning System (GPS) receiver, or a portable storage device (e.g., a universal serial bus (USB) flash drive), to name just a few.\|[0101] Computer-readable media suitable for storing computer program instructions and data include all forms of non-volatile memory, media, and memory devices, including by way of example semiconductor memory devices, e.g., EPROM, EEPROM, and flash memory devices; magnetic disks, e.g., internal hard disks or removable disks; magneto-optical disks; and CD-ROM and DVD-ROM disks. The processor and the memory can be supplemented by, or incorporated in special-purpose logic circuitry.\|[0102] To provide for interaction with a user, embodiments of the subject matter described in this specification can be implemented on a computer having a display device, e.g., a CRT (cathode ray tube) or LCD (liquid crystal display) monitor, for displaying information to the user and a keyboard and a pointing device, e.g., a mouse or a trackball, by which the user can provide input to the computer. Other kinds of devices can be used to provide for interaction with a user as well; for example, feedback provided to the user can be any form of sensory feedback, e.g., visual feedback, auditory feedback, or tactile feedback; and input from the user can be received in any form, including acoustic, speech, or tactile input. In addition, a computer can interact with a user by sending documents to and receiving documents from a device that is used by the user; for example, by sending web pages to a web browser on a user's user device in response to requests received from the web browser.\|[0103] Embodiments of the subject matter described in this specification can be implemented in a computing system that includes a back-end component, e.g., as a data server, or that includes a middleware component, e.g., an application server, or that includes a front-end component, e.g., a client computer having a graphical user interface or a Web browser through which a user can interact with an implementation of the subject matter described in this specification, or any combination of one or more such back end, middleware, or front end components. The components of the system can be interconnected by any form or medium of digital data communication, e.g., a communication network. Examples of communication networks include a local area network (“LAN”) and a wide area network (“WAN”), e.g., the Internet.\|[0104] The computing system can include clients and servers. A client and server are generally remote from each other and typically interact through a communication network. The relationship between client and server arises by virtue of computer programs running on the respective computers and having a client-server relationship with each other.\|[0105] While this specification contains many specific implementation details, these should not be construed as limitations on the scope of what may be claimed, but rather as descriptions of features that may be specific to particular embodiments. Certain features that are described in this specification in the context of separate embodiments can also be implemented in combination in a single embodiment. Conversely, various features that are described in the context of a single embodiment can also be implemented in multiple embodiments separately or in any suitable sub-combination. Moreover, although features may be described above as acting in certain combinations and even initially claimed as such, one or more features from a claimed combination can in some cases be excised from the combination, and the claimed combination may be directed to a sub-combination or variation of a sub-combination.\|[0106] Similarly, while operations are depicted in the drawings in a particular order, this should not be understood as requiring that such operations be performed in the particular order shown or in sequential order, or that all illustrated operations be performed, to achieve desirable results. In certain circumstances, multitasking and parallel processing may be advantageous. Moreover, the separation of various system components in the embodiments described above should not be understood as requiring such separation in all embodiments, and it should be understood that the described program components and systems can generally be integrated together in a single software product or packaged into multiple software products.\|[0107] Particular embodiments of the subject matter have been described. Other embodiments are within the scope of the following claims. For example, the actions recited in the claims can be performed in a different order and still achieve desirable results. As one example, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In certain implementations, multitasking and parallel processing may be advantageous. Other steps or stages may be provided, or steps or stages may be eliminated, from the described processes. Accordingly, other implementations are within the scope of the following claims.\|Terminology\|[0108] The phraseology and terminology used herein are for the purpose of description and should not be regarded as limiting.\|[0109] The term “approximately”, the phrase “approximately equal to”, and other similar phrases, as used in the specification and the claims (e.g., “X has a value of approximately Y” or “X is approximately equal to Y”), should be understood to mean that one value (X) is within a predetermined range of another value (Y). The predetermined range may be plus or minus 20%, 10%, 5%, 3%, 1%, 0.1%, or less than 0.1%, unless otherwise indicated.\|[0110] The indefinite articles “a” and “an,” as used in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.” The phrase “and/or,” as used in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Multiple elements listed with “and/or” should be construed in the same fashion, i.e., “one or more” of the elements so conjoined. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, a reference to “A and/or B”, when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A only (optionally including elements other than B); in another embodiment, to B only (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc.\|[0111] As used in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of,” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of,” “only one of,” or “exactly one of.” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law.\|[0112] As used in the specification and in the claims, the phrase “at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements. This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase “at least one” refers, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, “at least one of A and B” (or, equivalently, “at least one of A or B,” or, equivalently “at least one of A and/or B”) can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc.\|[0113] The use of “including,” “comprising,” “having,” “containing,” “involving,” and variations thereof, is meant to encompass the items listed thereafter and additional items.\|[0114] Use of ordinal terms such as “first,” “second,” “third,” etc., in the claims to modify a claim element does not by itself connote any priority, precedence, or order of one claim element over another or the temporal order in which acts of a method are performed. Ordinal terms are used merely as labels to distinguish one claim element having a certain name from another element having a same name (but for use of the ordinal term), to distinguish the claim elements.\|[0115] Each numerical value presented herein, for example, in a table, a chart, or a graph, is contemplated to represent a minimum value or a maximum value in a range for a corresponding parameter. Accordingly, when added to the claims, the numerical value provides express support for claiming the range, which may lie above or below the numerical value, in accordance with the teachings herein. Absent inclusion in the claims, each numerical value presented herein is not to be considered limiting in any regard.\|[0116] The terms and expressions employed herein are used as terms and expressions of description and not of limitation, and there is no intention, in the use of such terms and expressions, of excluding any equivalents of the features shown and described or portions thereof. In addition, having described certain embodiments of the invention, it will be apparent to those of ordinary skill in the art that other embodiments incorporating the concepts disclosed herein may be used without departing from the spirit and scope of the invention. The features and functions of the various embodiments may be arranged in various combinations and permutations, and all are considered to be within the scope of the disclosed invention. Accordingly, the described embodiments are to be considered in all respects as only illustrative and not restrictive. Furthermore, the configurations, materials, and dimensions described herein are intended as illustrative and in no way limiting. Similarly, although physical explanations have been provided for explanatory purposes, there is no intent to be bound by any particular theory or mechanism, or to limit the claims in accordance therewith.	(US20250164404)\|CROSS REFERENCE TO RELATED APPLICATION\|[0001] This application claims the benefit of U.S. Provisional Patent Application No. 63/601,059, titled “System and Method for Enhanced Rock Weathering Monitoring, Reporting, and Verification,” and filed on Nov. 20, 2023, the entire content of which is incorporated by reference herein.\|(US20250164404)\|TECHNICAL FIELD\|[0002] This disclosure relates to compositional characterization techniques, in particular, to optical devices that embody new methodologies for monitoring, reporting, and verification (MRV) of enhanced rock weathering (ERW).\|BACKGROUND\|[0003] Enhanced rock weathering (ERW) is the practice of applying crushed rocks and silicate minerals to agricultural land. It is a promising scalable and cost-effective carbon dioxide removal (CDR) strategy with significant environmental and agronomic co-benefits. However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions. Most current projects/systems/devices cannot accurately obtain carbon measurement and properly report carbon sequestration. Also, ERW lacks a robust monitoring, reporting, and verification (MRV) framework to address challenging problems such as carbon deception. For example, current MRV practices cannot provide a framework to easily detect and process a fraudulent claim of carbon gains by dishonest actors in the system.\|SUMMARY\|[0004] To address the aforementioned shortcomings, a method and a system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. The method include using a spectroscopy device to emit one or more optical signals directed to a target collected from a target area and to determine spectral measurements of the optical signals collected from the target. The method also includes using a data analysis subsystem to convert the spectral measurements to data indicating compositional characteristics of the target, analyze the data indicating compositional characteristics of the target using a plurality of analytical tools, and provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\|[0005] To convert the spectral measurements to the data indicating compositional characteristics of the target, one or more of the processes, such as determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. To determine the weathering status, loss of rock dust is determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering. To analyze the data indicating compositional characteristics, analytical tools are used to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS. To provide the assessment on carbon dioxide removal and insights on enhanced rock weathering, a prediction model is created to provide data support for subsequent implementation of enhanced rock weathering, and/or one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential are determined.\|[0006] In some embodiments, the heavy metal concentration is calculated in response to receiving bio-availability of metals and dissolved aqueous metals. In some embodiments, the soil organic carbon is measured based on determining the loss of material on ignition. In some embodiments, the target is a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered laser induced breakdown spectroscopy (LIBS) sampling. In some embodiments, the spectroscopy device is a handheld LIBS device. In some embodiments, the spectroscopy device is a LIBS device that is mounted on a motor vehicle and operates in real time as the motor vehicle traverses the target area, and the data analysis subsystem is integrated onboard the motor vehicle for real-time data acquisition and analysis. In some embodiments, the spectroscopy device is a LIBS device that is combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic from the target.\|[0007] The above and other preferred features, including various novel details of implementation and combination of elements, will now be more particularly described with reference to the accompanying drawings and pointed out in the claims. It will be understood that the particular methods and apparatuses are shown by way of illustration only and not as limitations. As will be understood by those skilled in the art, the principles and features explained herein may be employed in various and numerous embodiments.\|(US20250164404)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0008] The disclosed embodiments have advantages and features which will be more readily apparent from the detailed description, the appended claims, and the accompanying figures (or drawings). A brief introduction of the figures is below.\|[0009] FIG. 1A illustrates a block diagram of an exemplary ERW process.\|[0010] FIG. 1B illustrates a graphic representation of the speciation of a dominant form of dissolved carbon.\|[0011] FIG. 2A illustrates an overview of an exemplary laser induced breakdown spectroscopy (LIBS)-based data system, according to some embodiments.\|[0012] FIG. 2B illustrates an overall diagram of an exemplary LIBS device, according to some embodiments.\|[0013] FIG. 3 illustrates a block diagram of exemplary uses of LIBS devices in an MRV process for ERW, according to some embodiments.\|[0014] FIG. 4 illustrates a block diagram of exemplary features of LIBS devices and analysis used in MRV for ERW described in the present system, according to some embodiments.\|[0015] FIG. 5 illustrates a block diagram of exemplary data analysis and modeling used in the present system, according to some embodiments.\|[0016] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments.\|[0017] FIG. 7 illustrates a block diagram of an example computer system that may be used in implementing the technology described herein, according to some embodiments.\|(US20250164404)\|DETAILED DESCRIPTION\|[0018] The Figures (FIGs.) and the following description relate to preferred embodiments by way of illustration only. It should be noted that from the following discussion, alternative embodiments of the structures and methods disclosed herein will be readily recognized as viable alternatives that may be employed without departing from the principles of what is claimed.\|[0019] Reference will now be made in detail to several embodiments, examples of which are illustrated in the accompanying figures. It is noted that wherever practicable similar or like reference numbers may be used in the figures and may indicate similar or like functionality. The figures depict embodiments of the disclosed system (or method) for purposes of illustration only. One skilled in the art will readily recognize from the following description that alternative embodiments of the structures and methods illustrated herein may be employed without departing from the principles described herein.\|Scientific Introduction\|ERWA—A Durable Carbon Dioxide Removal Strategy\|[0020] Enhanced rock weathering (ERW) is a carbon dioxide removal (CDR) technique where naturally occurring mineral weathering reactions that consume atmospheric CO2 are accelerated. This may be achieved by applying crushed rocks and silicate minerals to agricultural soils. When the gradual rock dissolution or “weathering” occurs, alkaline minerals containing cations, such as calcium and magnesium (Ca2+ and Mg2+) that comprise the silicates, act as a pH amendment to remediate acidic soil on farms. In addition to balancing the pH of the soil, ERW can remove carbon dioxide from the atmosphere and sequester carbon for geological timescales.\|[0021] Basalt can be applied to managed land or an agricultural setting (e.g., rice paddies, corn fields, pasture lands) to practice ERW as a CDR strategy at scale. It should be recognized that the approach described herein is crop agnostic and can be generally applicable to any agricultural or managed land. As the dissolution of basalt proceeds, CO2 gas in the soil is converted to dissolved bicarbonate (HCO3−) in groundwater. This occurs due to basalt weathering reactions involving carbonic acid. Carbonic acid (H2O+CO2═H2CO3) is formed naturally in soils by plant respiration. The conversion of dissolved carbonic acid sources to bicarbonate draws CO2 down from the atmosphere.\|[0022] FIG. 1A illustrates a block diagram 100 of an exemplary ERW process. Basalt and/or other silicate materials (e.g., crushed rocks or “rock powder”) are applied to the soil and mixed into the subsurface near crops in 102. As the ERW progresses, the carbon dioxide (CO2 gas) from the respiration of roots 104 is converted to bicarbonate (HCO3−) in groundwater, and the CO2 stored in the soil 104 is also leached out of the soil and converted to bicarbonate. The bicarbonate is associated with a rising pH value of soil since the soil becomes less acidic. In this way, CO2 is removed. The silicate material application and CO2 isolation are associated with the deposition and sequestration processes 106, which results in the formation of weathering products in surface and groundwater runoff 108. Multiple enhanced rock weathering experiments have also demonstrated significant agronomic benefits due to improved nutrient supply for crops. Therefore, ERW deployments could aid farmers in regions where fertilizers are scarcely available or unaffordable.\|Carbon in Agricultural Setting\|[0023] The behavior of carbon in agricultural settings depends on the pH values in the settings. FIG. 1B illustrates a graphic representation 150 of the speciation of a dominant form of dissolved carbon, specifically, a representative calculation for the speciation of dissolved inorganic carbon (DIC). DIC is the sum of the aqueous species of inorganic carbon in a solution, which includes three major aqueous species: CO2, HCO3−, and CO32−. The speciation of DIC is the distribution of these species in a solution. The speciation of DIC can be determined by measuring the pH and total alkalinity of a solution and then using the measured values to calculate the concentrations of the different DIC species.\|[0024] To obtain the calculation demonstrating how the behavior of DIC changes with the pH value of soil in FIG. 1B, the pH value of the soil and pore waters of rice paddies is shifted towards pH=7 from ERW. As low pH (i.e., acidic) soils transition to neutral pH (i.e., pH≈7 ), dissolved CO2 is converted to the alkaline dissolved mineral bicarbonate (HCO3−). Near PH=7 bicarbonate is the dominant form of DIC. In other words, based on the shifting of the pH value, CO2 is converted to HCO3− and is not released as gas into the atmosphere.\|[0025] Next it is investigated what happens after CO2 is converted to other forms of dissolved inorganic carbon. After the conversion from CO2 to HCO3−, the bicarbonate (HCO3−) percolates into streams and rivers, from where the bicarbonate is delivered to the oceans. This DIC may reside in groundwater within the soil column for decades to centuries. This is an effective removal of carbon dioxide available to the ocean-atmosphere system. The eventual precipitation of bicarbonate as calcium carbonate minerals in deep aquifers or after transport to the ocean stably stores carbon for more than 10,000 years. The delivery of DIC to the ocean in the form of bicarbonate acts to enhance ocean alkalinity, which is vital for the health of ocean flora and fauna. For example, coral ecosystems have been particularly damaged by ocean acidification which is a well-known side effect of climate change. Ocean alkalinity enhancement works to counteract ocean acidification, as shown in 110 of FIG. 1A.\|Technical Problems\|[0026] It is hard to measure carbon capture. In agricultural and forest environments, many methods have been developed for measuring how much carbon is stored in soil. These methods significantly rely on labor-intensive mass-spectrometer measurements, spectroscopy, satellite-based sensors, and modeling. However, understanding the ecosystematic changes in soils is complex, as conditions may vary across a single plot of land. These methods cannot accurately evaluate carbon captured and retained in soils. Most current projects/methods cannot successfully quantify the amount of carbon, much less report carbon sequestration and conservation confidently. These schemes do not help address or incentivize emission avoidance and reduction by high-carbon industries (including agriculture).\|[0027] Even if the issue of carbon measurement can be solved, there are other challenges such as carbon deception. This is another main challenge related to the “net zero” demand in ecosystems. “Net zero” refers to a situation where an amount of carbon dioxide is removed from the atmosphere after that amount of carbon dioxide emission is generated, resulting in zero increase in net emissions. Thus, gas emission is still generated from human activity (e.g., fossil fuel companies can continue to explore, drill, extract, and burn fossil fuels), but carbon dioxide is taken out of the atmosphere in certain ways in some other places to balance out emissions. However dishonest actors may present during this procedure. For example, like a manufacturer rigging vehicles to cheat on emissions tests, forestry interventions may cut trees and then replant trees to claim carbon gains, i.e., carbon deception. Monitoring, reporting, and verification (MRV) is the process that can account for, communicate, and certify a CDR system's carbon removal over time. Currently, ERW lacks a robust MRV framework to obtain proper knowability of carbon sequestration (e.g., detecting carbon deception) and fill the knowledge gap to fulfill the demand of “net zero.”\|[0028] MRV is technically difficult due to the long timescales and uncertainties associated with the chemical and physical processes involved. Some crucial issues in MRV include accurately tracking carbon uptake, ensuring the permanence of carbon storage (e.g., long-time leakage risk), dealing with the variability of the process across different conditions, developing standardized reporting methods that ensure credibility and comparability across projects, etc. For example, there is no feasible way to directly measure the amount of CO2 removed from the atmosphere by ERW, and measuring CO2 in soils and groundwater is inherently challenging due to variability in environmental conditions (e.g., temperature, moisture levels, soil type, microbial activity). Emerging technologies (e.g., remote sensing, advanced soil sampling techniques) and research on effective MRV may help overcome some of the challenges.\|Overview\|[0029] The present disclosure proposes a novel system and method for performing compositional characterization of soil-rock dust mixtures. In some embodiments, the present system includes laser induced breakdown spectroscopy (LIBS) instruments that embody new MRV methodologies for ERW. LIBS deduces the elemental composition of a sample (e.g., solids, liquids, and gases) from measurements of the spectral line emission emitted by the plasma produced by high-power laser irradiation of the sample. LIBS will be described in further detail below.\|[0030] In some embodiments, the proposed workflow as described herein may include four primary facets:\| - i. Choose where to sample and measure compositional characteristics of soils;\| - ii. Determine how to measure compositional characteristics of the soils using LIBS;\| - iii. Analyze LIBS measurements (e.g., based on existing gold-standard measurement techniques); and\| - iv. Use post-processing analytical tools to create high-quality, verifiable carbon credits (a tradable certificate used to reduce global greenhouse gas emissions).\|[0035] The present disclosure also proposes multiple LIBS devices that may be employed in the field, workstations, or laboratories.\|[0036] FIG. 2A illustrates an overview of an exemplary LIBS-based data system 200 that is used to implement the functionalities described herein. In this example, system 200 includes a sample handling unit 202, a LIBS device 204, and a data processing unit 206. System 200 may use sample handling unit 202 to identify locations or zones that target samples (e.g., soil samples) should be collected from (e.g., geolocated zone-based soil sampling). Depending on different quantitative analyses and qualitative analyses to be performed (e.g., as described in FIGS. 3-6), sample handling unit 202 may also be used to instruct LIBS device 204 to obtain specific types of measurements. The present system may further use sample handling unit 202 to ensure the accurate positioning of a sample for optical interaction with LIBS device 204. LIBS device 204 is employed to obtain measurements and analysis data from samples, which will be described in detail in FIG. 2B. The data from LIBS device 204 is further analyzed and modeled by data processing unit 206 for the purpose of monitoring, reporting, and verification, for example, as illustrated in FIG. 5 below. Although only one LIBS device is shown in the example system 200 of FIG. 2A, it is possible that more LIBS devices and/or other units/components may be included in a LIBS-based data system.\|[0037] In some embodiments, at least a portion of the data processing unit 206 is part of a computer system (described below in FIG. 7) that is communicatively coupled to LIBS device 204. In other embodiments, at least a portion of the data processing unit 206 may be integrated into LIBS device 204. For example, data processing unit 206 may reside on a standalone computer system to perform advanced compositional analysis based on real-time sample analysis from data acquisition & analysis component 260 of LIBS device 204 (described below in FIG. 2B). Data processing unit 206 together with data acquisition & analysis component 260 form a data analysis subsystem that is responsible for various types of data processing, evaluation, calculation, etc, as described in the present disclosure. When LIBS device 204 is attached to or mounted on a motor instrument (e.g., vehicle, drone), the data analysis subsystem may be integrated into data acquisition onboard the motor instrument for real-time data acquisition and analysis. In some embodiments, at least a portion of the sample handling unit 202 may also be part of an external computer system and/or an integrated part of LIBS device 204. For example, sample handling unit 202 may be designed to use motorized stages or robots to move a sample in a controlled manner and thus is included in or attached to LIBS device 204 for precise sample positioning.\|LIBS Device\|[0038] LIBS is a rapid chemical analysis technology that uses a short laser pulse to create a micro-plasma on the sample surface. LIBS can be used to detect the presence of various elements in a sample based on directing a high-power emission from a laser onto the sample to form a plasma. The plasma is then analyzed spectroscopically to determine the composition of the sample. The LIBS is often used with a soil penetrating probe to detect heavy metal contamination in soil due to its high sensitivity and sample-free preparation. The LIBS analytical technique offers some other compelling advantages such as fast measurement time (e.g., a few seconds for a single spot analysis), broad elemental coverage (e.g., including, but not limited to, lighter elements such as H, Be, Li, C, N, O, Na, and Mg), versatile sampling protocols that include fast raster of the sample surface and depth profiling, etc.\|[0039] The present disclosure proposes new LIBS device(s) used in the MRV process for ERW. In some embodiments, the new LIBS device is a single multi-purpose optical device. In other embodiments, the new LIBS device may include one or more optical devices. Each device can be designed for a single purpose or multiple purposes. The LIBS devices may have various physical components and/or configurations.\|[0040] FIG. 2B illustrates an overall block diagram of an exemplary LIBS device 204, which includes some key components such as optical source 254, focusing and light collection optics 256, detector 258, and data acquisition & analysis component 260. These components are depicted merely for illustration, and other components (more or less) may be included in LIBS device 204. For example, sample probe 252 may be part of the LIBS device 204. In some embodiments, LIBS device 204 may use a sample probe 252 (e.g., a soil penetrating probe) to take a sample from a target area that is strategically identified (e.g., on managed land). In response, optical source 254 (e.g., a laser) may generate a high-energy light pulse that is directed onto the sample, and focusing and light collection optics 256 (e.g., lens, mirrors) may focus the light pulse to a specific point on the sample, thereby creating a plasma plume. The focusing and light collection optics 256 may also capture/collect the light pulse/beam to avoid light interference. The collected light pulse is then passed through detector 258 (e.g., spectrometer) to obtain sample measurements (e.g., spectral data). For example, detector 258 may disperse the light pulse into individual wavelengths, determine the intensity of light at each wavelength (e.g., using a charge-coupled device (CCD) or photo-multiplier tube (PMT)), and generate a spectrum that is characteristic of specific elements in the sample.\|[0041] Data acquisition & analysis component 260 may include computing hardware such as a central processing unit, memory, and storage, as described in the computer system of FIG. 7. Data acquisition & analysis component 260 is configured to receive the measurement data from detector 258 and perform the elemental composition analysis on the measurement data. In some embodiments, LIBS device 204 may also communicate with an alternative or additional data processing unit (e.g., 206) to perform LIBS analysis and any other elemental identification and quantification analyses. Based on the analysis, a result is generated in 262. For example, the result may be a report or graphical output showing the elemental composition of the sample. Various types of measurements and analyses may be conducted by the data analysis subsystem including data acquisition & analysis component 260 and data processing unit 206, which will be further described below with reference to FIGS. 3-6.\|[0042] The present system may deploy one or more improved LIBS devices to implement the disclosed functionalities. For example, the improved LIBS device (e.g., 204) may be equipped, attached, or associated with an autofocusing component to enable consistent, in-focus measurements of samples without moving other optical components. The autofocusing component may be included as a part of a suitable optical assembly that is hand-held, attached to a mobile vehicle, or integrated with a positioning system (e.g., robotic arm, boom, leg, conveyor belt), etc. Using the autofocusing component, spectroscopy measurements can be automatically focused based on a focal length of its optics relative to the target sample. Instead of using certain mechanisms (e.g., mechanical actuators) to change the position of the optical component(s), in some embodiments, the autofocusing component may include a shape changing lens (e.g., variable focus lens) to allow continuous tuning of a focal length and working distance of the autofocusing component relative to a target sample.\|Data Acquisition and Evaluation Using LIBS Device\|[0043] As discussed above, components 252, 254, 256, 258, and/or 260 of LIBS device 204 may work together with other units of data system 200 to acquire sample data and provide insights about the elemental composition of a sample (e.g., soil sample). In the illustrated embodiment of FIG. 3, one or more LIBS devices 204 may be used to determine weathering status 304, evaluate specific soil contents/elements 306, calculate heavy metal concentration 308, evaluate metal ratios in soils 310, and/or measure soil organic carbon 312. In some embodiments, one or more LIBS devices 200 may also be used to measure and analyze the compositional characteristics of soils, the biological composition of plant and seed matter, and the elemental composition of rock samples.\|[0044] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) used for determining weathering status 304. In some embodiments, a LIBS-based device may be employed to assess the composition of lighter cations relative to heavier cations in applied rock dust. This composition analysis may be used in determining the weathering status of the rock dust application on agricultural fields, pasture lands, or any other natural environments. Thus, an approach is obtained, for determining the loss of rock dust due to enhanced rock weathering (ERW) for the purpose of monitoring, reporting, and verification (MRV) to create carbon credits.\|[0045] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating specific soil elements 306, for example, the nitrogen (N), phosphorus (P), and potassium (K) content of the soil. This is the estimation of nutrient requirements, factoring in additional nutrients provided by rock dust application. The use of LIBS devices in elemental composition analysis can reduce farmers' burden to apply fertilizers (i.e., NPK nitrogen-phosphorus-potassium) while conducting ERW projects. LIBS allows the quantification of these additional bioavailable nutrients, which become active in the soil column with the breakdown of the rock minerals (e.g., being modified through chemical, physical, or biological interactions with rocks and minerals).\|[0046] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for calculating heavy metal concentrations 308, e.g., the amounts of metallic elements (often toxic) found in the soils or rock dust used for ERW. These elements may include metals such as lead (Pb), mercury (Hg), nickel (ni), etc., and can be found in pesticides, fertilizers, or untreated sewage sludge introduced into the soil. The heavy metal may accumulate in the environment to pose serious health and ecological risks. The disclosed LIBS device may provide insights into the safety considerations of cultivating various crops, for example, providing insights into phytoremediation such as using sunflowers to remove Strontium, which is poisonous metal to most other livings. According to US Environmental Protection Agency (EPA) standards, the bio-availability of metals and dissolved aqueous metals will be needed for calculating heavy metal concentrations.\|[0047] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for evaluating key metal ratios in soils for ERW 310. In some embodiments, critical metal ratios in soils are assessed using LIBS technology before the implementation of ERW (i.e., before the rock dust application for enhanced weathering). This process can be outlined as follows:\| - i. Sample Collection: soil samples are collected from the target area where ERW is planned. These samples represent the current soil composition in the region;\| - ii. LIBS Analysis: the collected soil samples are subjected to LIBS analysis. The LIBS device measures the elemental composition of the soil, providing baseline data on the concentrations of various metals being present;\| - iii. Trace metal ratios and potential pulverized rock dust field amendments may then be evaluated together to determine if the rock dust is appropriate for application to the field; and \| - a. Evaluate environmental concerns,\| - b. Evaluate the potential for signal strength in measurements: measuring key metal ratios for MRV process.\| - iv. Key Metal Ratios: specific metal ratios of interest, which are known to influence the effectiveness of ERW, are calculated based on the LIBS data. These key metal ratios often include ratios such as calcium to magnesium (Ca/Mg), calcium to potassium (Ca/K), or calcium to sodium (Ca/Na), among others.\|[0054] In some embodiments, the calculated key metal ratios are evaluated to determine the suitability of the soil for ERW. An ideal balance of these ratios is typically necessary for optimal carbon capture and weathering outcomes. The assessment results may guide decisions regarding the need for rock dust application and the specific rock dust type required to achieve the desired metal ratios for effective ERW.\|[0055] By employing LIBS technology for the evaluation of key metal ratios in soils before rock dust application for enhanced weathering, informed decision-making can be used to ensure that the chosen ERW strategy is tailored to the specific soil composition of the target area. This optimization may also contribute to efficient carbon dioxide removal and MRV.\|[0056] In some embodiments, the present disclosure describes a LIBS device (e.g., 204) for measuring soil organic carbon 312. A LIBS device can be used to measure soil organic carbon (SOC) levels. The SOC level represents the amount of carbon stored in the form of organic compounds in the soil, and SOC is critical to soil quality and carbon sequestration because it helps store carbon from the atmosphere and contributes to mitigating climate change. By measuring the SOC level, the present disclosure facilitates the correlation between changes in organic carbon attributable to rock dust application, thereby offering valuable insights into soil improvement. In some embodiments, soil organic carbon measurements may be approximated by the loss of material on ignition (LOI) (e.g., by measuring the weight loss of organic matter content after heating the sample to a high temperature).\|LIBS Analysis\|[0057] Numerous LIBS analyses may be conducted based on element measurements, calculation, and evaluation. In addition to in-depth soil analysis, when a LIBS device is used to measure the biological composition of plant and seed matter, the LIBS analysis can serve to validate the absence of potential metal accumulation resulting from enhanced weathering processes.\|[0058] In some embodiments, a LIBS device may also be used for rock sample analysis, where the elemental composition of raw rock samples from rock quarries or in the field is analyzed. This LIBS analysis may be applied to determine an enhanced weathering potential and a total carbon dioxide removal (CDR) potential. The enhanced weathering potential is the amount of atmospheric carbon dioxide that can be removed and stored through the ERW process (e.g., manual application of rocks or minerals) over a specific period of time. This factor may vary depending on the type of rocks/minerals used in ERW, the surface area available for reaction, environmental conditions (e.g., precipitation, temperature), etc. The total CDR potential is the amount of carbon dioxide that can be removed from the atmosphere in the long term, which depends on the effectiveness of the ERW process.\|[0059] In some embodiments, a spectral fluorescence device may be used in combination with LIBS analysis to create a dual system. This dual system enables the simultaneous determination of organic carbon and elemental composition in samples. This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status. In some embodiments, this approach may also be used to help refine soil organic carbon estimates outlined in 312 of FIG. 3. In general, the combination of LIBS and fluorescence may expand and strengthen the LIBS measurement and analysis, e.g., as discussed in FIG. 3.\|Beneficial Features of LIBS Device and Analysis\|[0060] FIG. 4 illustrates a block diagram 400 of exemplary features of LIBS devices and analysis used in the MRV process for ERW as described in the present system.\|[0061] The present system allows improved statistical accuracy with pooled/composite soil samples, as shown in 402. By aggregating soil samples from various locations within a field, the present system seeks to accurately determine the central compositional tendency and associated dispersion or variance in the soil's elemental composition. As compared to the current techniques, the utilization of pooled samples enables a more robust and representative analysis of the soil's overall composition, contributing to a more precise assessment of soil quality and environmental conditions. The accurate measurement of pooled samples is particularly important to soil fertility assessment, soil quality monitoring, and precision agriculture.\|[0062] The present system provides geolocated zone-based soil sampling for target characteristic assessment, as shown in 404. In some embodiments, the present system allows the collection of soil samples from specific geolocated zones within a field. By strategically pooling samples from these distinct zones, the analysis can yield precise data regarding the central tendency and variance of the target characteristic within each zone. This geolocated zone-based sampling approach offers a granular understanding of the spatial heterogeneity, distribution, and variability of the target characteristic, thereby enabling informed decision-making for soil management and ERW applications. Potential future obstacles with a MRV process based on soil heterogeneity may also be addressed by examining measurements at this juncture. In some embodiments, zones may be determined based on soil type, gridded areas, etc. A zone may also be small, predefined regions that include, but are not limited to, a circular region with a predefined radius or a square area with a predefined side length.\|[0063] The LIBS device of the present system can be used in rock sample analysis to determine enhanced weathering potential and total carbon dioxide removal (CDR) potential. In particular, the present system may evaluate the carbon dioxide potential of alkaline silicate minerals, as shown in 406. The present system can assess the carbon dioxide potential of alkaline silicate minerals including, but not limited to, basalt, olivine, and wollastonite. These minerals are known for their capacity to sequester carbon dioxide through enhanced weathering processes. In some embodiments, the present system may utilize a LIBS device to analyze the elemental composition of these minerals and determine their specific potential for CDR. By accurately quantifying the CDR potential of alkaline silicate minerals, the present system gains valuable insights into the efficacy of a CDR solution.\|[0064] The present system allows systematic preparation of pressed-pelletized subsamples derived from pooled soil samples, as shown in 408. By compressing and pelletizing soil material from each pooled sample, the present system may create a consistent and standardized substrate for LIBS analysis. This process can minimize variations in sample presentation, ensuring reliable and reproducible results during LIBS analysis. This process further streamlines the handling of samples, allowing for an efficient assessment of the central compositional tendency and variance of the target characteristics within the soil, and ultimately enhancing the accuracy of soil quality and environmental assessments.\|[0065] The present system further allows grid-based or rastered LIBS sampling for in-depth soil core analysis, as shown in 410. In some embodiments, the present system may conduct grid-based or rastered analyses of the pelletized subsamples, where the LIBS device systematically scans and analyzes discrete regions or points on the pellet surface in a structured grid or raster pattern. This approach enables a comprehensive examination of the intersample heterogeneity (or microheterogeneity) of soil characteristics and the distribution of elemental composition within the subsamples.\|[0066] Through this analysis, the present system may achieve a high-resolution understanding of the central compositional tendency and variance of the target characteristics in the soil, and the detailed information may provide invaluable insights into the spatial variability of soil properties, thereby enhancing precision in soil quality assessment and MRV for CDR applications.\|[0067] Using rasterized or gridded LIBS sampling can also systematically measure the elemental composition of intact soil cores at various depths. By taking measurements in a prescribed structured grid or raster pattern for LIBS analysis along the length of an intact soil core, the present approach enables precise characterization of the compositional variations with depth. This is particularly beneficial for understanding how soil properties change at different depths within the core, offering crucial insights into subsurface composition and environmental conditions. The present system seeks to assess soil heterogeneity and geological attributes with depth, contributing to informed decisions in ERW applications and MRV techniques.\|Device Characteristics and Deployment\|[0068] The present system supports specific device characteristics and deployment that are beneficial to the MRV process for ERW. In some embodiments, the present system supports handheld and miniaturized LIBS devices for soil sampling, field-based depth-integrated soil profiling with LIBS and soil auger, and in-field deployment of LIBS technology on motor vehicles, etc.\|[0069] The LIBS device described herein can be a handheld device that is portable, easy to operate, and suitable for rapid data acquisition. This handheld device is particularly useful in patchwork small-holder farms (e.g., rice paddies). It is engineered to provide a simplified user interface while maintaining the analytical accuracy and precision required for soil and environmental analysis. Any instantiation of the LIBS device may contain fewer optical sensors than the original, making the device more affordable and lighter. As a result, this LIBS device is adaptive for use in rural, remote, and economically disadvantaged communities. In addition, the miniaturized form of the device enables the present system to perform real-time, in-situ analyses, contributing to timelier and data-driven decision-making processes in agriculture, geology, and environmental science.\|[0070] The present system also allows a LIBS device to be combined with a soil auger to obtain a depth-integrated soil profile of a predetermined target characteristic. A soil auger is employed to collect soil samples at various depths within the field. These samples are representative of the soil composition at specific depth intervals.\|[0071] After and/or during the auguring process, the present system performs LIBS analysis on the collected soil samples. A LIBS device can rapidly and accurately measure the elemental composition of the soil samples, including the concentration of the target characteristic of interest. The present system may then integrate the LIBS data obtained from each depth interval to construct a depth-integrated soil profile of the target characteristic. This profile provides a comprehensive understanding of how the target characteristic varies with depth within the soil.\|[0072] A LIBS device/instrument can be deployed in different ways. In some embodiments, the present system supports in-field deployment of LIBS technology on motor vehicles. LIBS is integrated into motor vehicles, such as tractors or other agricultural machinery, for in-field deployment. The present system seamlessly integrates LIBS instrumentation into the design of motor vehicles used for field operations, such as tractors.\|[0073] The LIBS device can be securely mounted, ensuring stability during vehicle movement. The LIBS device may operate in real time as the motor vehicle traverses the field. The LIBS device continuously analyzes the soil or other target materials as the vehicle moves, providing instant elemental composition data. The present system may collect LIBS-generated data and integrate the data into a data acquisition (DAQ) onboard the vehicle, allowing for real-time decision-making based on soil or material composition. A vehicle operator can use the LIBS data to make immediate adjustments to field operations for any ERW-related purpose, such as varying fertilizer application rates or adjusting rock dust application rates based on the in-field analysis. The present system may log the LIBS data, providing a detailed record of the soil or material composition across the field for subsequent analysis and optimization.\|[0074] In some embodiments, the present system may support other deployment methods. For example, one or more LIBS devices may be integrated into drones, underwater vehicles/amphibious, or other mobil instruments.\|Data Analysis and Modeling\|[0075] FIG. 5 illustrates a block diagram 500 of exemplary features of data analysis and modeling used in the present system. As depicted in FIG. 5, the data analysis and modeling 502 of the present system may be featured with various analytical tools such as multivariate distribution modeling for cation covariance analysis 504, empirical modeling for weathering prediction and carbon credit creation 506, calibration with high-precision inductively coupled plasma mass spectrometers (ICP-MS) data 508, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS 510, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV 512. In some embodiments, these data analyses and modeling may be performed at least by data processing unit 206 in combination with data acquisition & analysis component 260 as shown in FIGS. 2A and 2B (i.e., data analysis subsystem).\|[0076] The present system provides multivariate distribution modeling for cation covariance analysis, as shown in 504. In some embodiments, the LIBS data can be leveraged for analyzing and modeling the covariance relationships among key cations in soil including, but not limited to, titanium, calcium, sodium, magnesium, potassium, phosphorous, and nitrogen. In some embodiments, the present system entails fitting multivariate normal or non-normal distributions to the data obtained through LIBS measurements.\|[0077] Multivariate distribution fitting allows for the comprehensive assessment of the covariance and correlations between key cations in soil. It provides valuable insights into the simultaneous variations and relationships among these elements, contributing to a deep understanding of soil composition and baseline information required for MRV. The present system uses LIBS to provide dense and rapid enough data to find systematic variances in soil heterogeneity within any given field, pasture, agricultural setting, or any other natural setting.\|[0078] In some embodiments, the present system may apply the quantitative elemental analysis approach as described in Sobron, titled “non-linear methods for quantitative elemental analysis and mineral classification using laser-induced breakdown spectroscopy (LIBS),” U.S. patent application Ser. No. 15/998,391, which is hereby incorporated by reference in its entirety.\|[0079] In some embodiments, the present system supports empirical modeling for weathering prediction and carbon credit creation, as shown in 406. That is, data collected in the present system can be leveraged to develop an empirically driven model for predicting the weathering of rock dust applied to fields and providing suggestions and instructions for subsequent ERW implementation.\|[0080] The empirical model may help the monitoring, reporting, and verification (MRV) process, which aims at quantifying the carbon capture potential resulting from enhanced weathering practices. By using dense, LIBS-generated data to create a predictive model, it becomes possible to monitor and report on the efficiency of carbon capture using regression-based and/or machine-learning methods. As a result, the time between data collection and sales for creating carbon credits may be reduced. The empirically driven model therefore facilitates accurate and data-driven MRV processes while incentivizing an easy switch to practices where carbon credits may be created through ERW. For example, when structure a predictive model, the present system may use mineral type, application rate, surface area of mineral, climate data, and environmental carbon dioxide concentration as input parameters of the model. The present system may calculate the weathering rate based on the environmental conditions and mineral properties, calculate the sequestration of carbon dioxide, and use weathering rate equations to predict how much carbon dioxide may be captured within a specific area over a specific timeframe. The present system may also calculate the total carbon dioxide removal rate to estimate global or regional carbon dioxide sequestration potential.\|[0081] To ensure accuracy and precision, in some embodiments, the present system may calibrate the LIBS device using high-precision measurements obtained from ICP-MS, as shown in 508.\|[0082] ICP-MS represents a well-established and highly accurate analytical technique, known for its exceptional precision in measuring elemental composition. By calibrating the LIBS device against ICP-MS data, the present system may establish a robust and reliable calibration framework. This calibration method may serve to validate and fine-tune the LIBS measurements, ensuring accuracy and traceability to a gold standard in elemental analysis.\|[0083] The integration of ICP-MS calibration in the present system enhances the trustworthiness and consistency of LIBS measurements, and the enhanced measurements may be suitable for a wide range of ERW applications for MRV. This calibration approach boosts the credibility of LIBS technology in scientific research and regulatory compliance (e.g., metals contamination according to EPA standards).\|[0084] The present system supports the construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, as shown in 510. In some embodiments, the present system may use known mixtures of soil and rock dust to create calibration curves. With a soil sample and rock dust sample that have already been characterized via ICP-MS or other analytical techniques, the present system can obtain known mixtures such that the rock dust comprises a known percentage of the weight of a newly created sample. By testing many mixed samples using LIBS with an array of rock dust ranging from 0 to 100% weight by mass, the present system can determine a series of calibration curves. These curves may fit the compositional characteristics of a particular soil type-rock dust combination. The present system may then store the data for soil type-rock dust combinations, creating a large database of possible LIBS spectral signals for a range of possible compositional arrays. With a sufficiently large database, the present system can apply one or more regression-based, machine-learning-based tools, and principal component analysis to select the most optimal calibration curve for new measurement(s).\|[0085] Here, the present system aims to strengthen the credibility of carbon credit generation. In some embodiments, the present system may use the misfit of measurements to known calibration curves to quantify measurement uncertainty, so that carbon credit sales effectively incorporate potential variations in carbon capture into pricing structures.\|[0086] In some embodiments, the present system supports collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS for CDR MRV, as shown in 512. In other words, ICP-MS and LIBS are used collaboratively to spot-check and validate the empirically driven model developed for CDR MRV. This process ensures that the model accurately reflects the carbon capture and sequestration processes in real-world applications, enhancing the reliability of carbon credit generation. The present system may also use the same collaborative framework to generate uncertainty models when upscaling the sample area for MRV. To upscale the sample area for MRV, test plots are used to make projections for larger fields, and/or several fields are used to project CDR for a region, etc. By systematically assessing variations and uncertainties using ICP-MS and LIBS data, these models provide insights into the potential variability in carbon capture estimates as the sample area is expanded. This information is essential for accurately quantifying carbon credits and assuaging buyers' concerns about the quality of carbon credits. The information is also crucial to assess the quality of MRV.\|[0087] The present system aims to strengthen the credibility of carbon credit generation and improve informed decision-making in ERW-related land management. By integrating uncertainty modeling, the present system enhances its ability to account for variations in carbon capture and carbon dioxide removal potential and provides a comprehensive assessment of carbon dioxide removal efforts. The present system may enhance the credibility of carbon credit generation while providing transparency and accountability in environmental initiatives.\|Flowchart\|[0088] FIG. 6 illustrates a flowchart 600 of monitoring, reporting, and verification of enhanced rock weathering, according to some embodiments. Method 600 may be implemented using a LIBS-based data system 200, as shown in FIGS. 2A and 2B. A spectroscopy device (e.g., LIBS device 204) is used to obtain measurements from a target sample. At step 602, the spectroscopy device (e.g., using optical source 254) emits one or more optical signals directed to a target collected from a target area (e.g., managed field or other agricultural settings). At step 604, the spectroscopy device (e.g., using detector 258) determines spectral measurements of the optical signals collected from the target. The target can be a pooled sample that includes soil samples collected and combined from multiple locations within the target area. One or more geolocated zones within the target area may be identified (e.g., by sample handing unit 202) from which the pooled sample is collected, and the pooled sample is collected from the target area using grid-based or rastered LIBS sampling.\|[0089] As shown in FIGS. 2A and 2B, a data analysis subsystem (e.g., including data processing unit 206 and data acquisition & analysis component 260) is communicatively coupled to the spectroscopy device (e.g., LIBS device 204). At step 606, the data analysis subsystem is configured to convert the spectral measurements to data indicating compositional characteristics of the target, which includes at least one or more of determining a weathering status, evaluating target contents, calculating heavy metal concentration, determining metal ratios in the target, or measuring organic carbon in the target, are performed. For example, to determine the weathering status, loss of rock dust may be determined by assessing the composition of cations in rock dust applied to the target area through the enhanced rock weathering.\|[0090] The data analysis subsystem is then configured to analyze the data indicating compositional characteristics of the target using a plurality of analytical tools at step 608, and provide assessment on carbon dioxide removal and insights on enhanced rock weathering at step 610. In some embodiments, to analyze the compositional data, the data analysis subsystem uses various analytical tools to perform one or more of multivariate distribution modeling for cation covariance analysis, empirical modeling for weathering prediction and carbon credit creation, calibration with high-precision ICP-MS data, construction of calibration curves for soil-rock dust mixtures with high-precision ICP-MS, and collaborative spot-checking and uncertainty modeling with ICP-MS and LIBS, etc. To provide the assessment, the data analysis subsystem may also calculate one or more of an enhanced weathering potential and a total carbon dioxide removal (CDR) potential.\|Computer Implementation\|[0091] In some examples, some or all of the processing described above can be carried out on a personal computing device, on one or more centralized computing devices, or via cloud-based processing by one or more servers. Some types of processing can occur on one device and other types of processing can occur on another device. Some or all of the data described above can be stored on a personal computing device, in data storage hosted on one or more centralized computing devices, and/or via cloud-based storage. Some data can be stored in one location and other data can be stored in another location. In some examples, quantum computing can be used, and/or functional programming languages can be used. Electrical memory, such as flash-based memory, can be used.\|[0092] FIG. 7 is a block diagram of an example computer system 700 that may be used in implementing the technology described herein. General-purpose computers, network appliances, mobile devices, or other electronic systems may also include at least portions of the system 700. The system 700 includes a processor 710, a memory 720, a storage device 730, and an input/output device 740. Each of the components 710, 720, 730, and 740 may be interconnected, for example, using a system bus 750. The processor 710 is capable of processing instructions for execution within the system 700. In some implementations, the processor 710 is single-threaded. In some implementations, the processor 710 is a multi-threaded processor. The processor 710 is capable of processing instructions stored in the memory 720 or on the storage device 730.\|[0093] Memory 720 stores information within the system 700. In some implementations, the memory 720 is a non-transitory computer-readable medium. In some implementations, the memory 720 is a volatile memory unit. In some implementations, the memory 720 is a non-volatile memory unit.\|[0094] The storage device 730 is capable of providing mass storage for the system 700. In some implementations, the storage device 730 is a non-transitory computer-readable medium. In various implementations, the storage device 730 may include, for example, a hard disk device, an optical disk device, a solid-state drive, a flash drive, or some other large-capacity storage device. For example, the storage device may store long-term data (e.g., database data, file system data, etc.). The input/output device 740 provides input/output operations for the system 700. In some implementations, the input/output device 740 may include one or more network interface devices, e.g., an Ethernet card, a serial communication device, e.g., an RS-232 port, and/or a wireless interface device, e.g., an 802.11 card, a 3G wireless modem, or a 4G wireless modem. In some implementations, the input/output device may include driver devices configured to receive input data and send output data to other input/output devices, e.g., keyboard, printer, and display devices 760. In some examples, mobile computing devices, mobile communication devices, and other devices may be used.\|[0095] In some implementations, at least a portion of the approaches described above may be realized by instructions that upon execution cause one or more processing devices to carry out the processes and functions described above. Such instructions may include, for example, interpreted instructions such as script instructions, executable code, or other instructions stored in a non-transitory computer-readable medium. The storage device 730 may be implemented in a distributed way over a network, such as a server farm or a set of widely distributed servers, or may be implemented in a single computing device.\|[0096] Although an example processing system has been described in FIG. 7, embodiments of the subject matter, functional operations, and processes described in this specification can be implemented in other types of digital electronic circuitry, in tangibly embodied computer software or firmware, in computer hardware, including the structures disclosed in this specification and their structural equivalents, or in combinations of one or more of them. Embodiments of the subject matter described in this specification can be implemented as one or more computer programs, i.e., one or more modules of computer program instructions encoded on a tangible nonvolatile program carrier for execution by, or to control the operation of, data processing apparatus. Alternatively or in addition, the program instructions can be encoded on an artificially generated propagated signal, e.g., a machine-generated electrical, optical, or electromagnetic signal that is generated to encode information for transmission to a suitable receiver apparatus for execution by a data processing apparatus. The computer storage medium can be a machine-readable storage device, a machine-readable storage substrate, a random or serial access memory device, or a combination of one or more of them.\|[0097] The term “system” may encompass all kinds of apparatus, devices, and machines for processing data, including by way of example a programmable processor, a computer, or multiple processors or computers. A processing system may include special-purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit). A processing system may include, in addition to hardware, code that creates an execution environment for the computer program in question, e.g., code that constitutes processor firmware, a protocol stack, a database management system, an operating system, or a combination of one or more of them.\|[0098] A computer program (which may also be referred to or described as a program, software, a software application, a module, a software module, a script, or code) can be written in any form of programming language, including compiled or interpreted languages, or declarative or procedural languages, and it can be deployed in any form, including as a standalone program or as a module, component, subroutine, or other unit suitable for use in a computing environment. A computer program may, but need not, correspond to a file in a file system. A program can be stored in a portion of a file that holds other programs or data (e.g., one or more scripts stored in a markup language document), in a single file dedicated to the program in question, or in multiple coordinated files (e.g., files that store one or more modules, sub programs, or portions of code). A computer program can be deployed to be executed on one computer or on multiple computers that are located at one site or distributed across multiple sites and interconnected by a communication network.\|[0099] The processes and logic flows described in this specification can be performed by one or more programmable computers executing one or more computer programs to perform functions by operating on input data and generating output. The processes and logic flows can also be performed by, and apparatus can also be implemented as, special purpose logic circuitry, e.g., an FPGA (field programmable gate array) or an ASIC (application-specific integrated circuit).\|[0100] Computers suitable for the execution of a computer program can include, by way of example, general or special purpose microprocessors or both, or any other kind of central processing unit. Generally, a central processing unit will receive instructions and data from a read-only memory, a random access memory, or both. A computer generally includes a central processing unit for performing or executing instructions and one or more memory devices for storing instructions and data. Generally, a computer will also include, or be operatively coupled to receive data from or transfer data to, or both, one or more mass storage devices for storing data, e.g., magnetic, magneto-optical disks, or optical disks. However, a computer need not have such devices. Moreover, a computer can be embedded in another device, e.g., a mobile telephone, a personal digital assistant (PDA), a mobile audio or video player, a game console, a Global Positioning System (GPS) receiver, or a portable storage device (e.g., a universal serial bus (USB) flash drive), to name just a few.\|[0101] Computer-readable media suitable for storing computer program instructions and data include all forms of non-volatile memory, media, and memory devices, including by way of example semiconductor memory devices, e.g., EPROM, EEPROM, and flash memory devices; magnetic disks, e.g., internal hard disks or removable disks; magneto-optical disks; and CD-ROM and DVD-ROM disks. The processor and the memory can be supplemented by, or incorporated in special-purpose logic circuitry.\|[0102] To provide for interaction with a user, embodiments of the subject matter described in this specification can be implemented on a computer having a display device, e.g., a CRT (cathode ray tube) or LCD (liquid crystal display) monitor, for displaying information to the user and a keyboard and a pointing device, e.g., a mouse or a trackball, by which the user can provide input to the computer. Other kinds of devices can be used to provide for interaction with a user as well; for example, feedback provided to the user can be any form of sensory feedback, e.g., visual feedback, auditory feedback, or tactile feedback; and input from the user can be received in any form, including acoustic, speech, or tactile input. In addition, a computer can interact with a user by sending documents to and receiving documents from a device that is used by the user; for example, by sending web pages to a web browser on a user's user device in response to requests received from the web browser.\|[0103] Embodiments of the subject matter described in this specification can be implemented in a computing system that includes a back-end component, e.g., as a data server, or that includes a middleware component, e.g., an application server, or that includes a front-end component, e.g., a client computer having a graphical user interface or a Web browser through which a user can interact with an implementation of the subject matter described in this specification, or any combination of one or more such back end, middleware, or front end components. The components of the system can be interconnected by any form or medium of digital data communication, e.g., a communication network. Examples of communication networks include a local area network (“LAN”) and a wide area network (“WAN”), e.g., the Internet.\|[0104] The computing system can include clients and servers. A client and server are generally remote from each other and typically interact through a communication network. The relationship between client and server arises by virtue of computer programs running on the respective computers and having a client-server relationship with each other.\|[0105] While this specification contains many specific implementation details, these should not be construed as limitations on the scope of what may be claimed, but rather as descriptions of features that may be specific to particular embodiments. Certain features that are described in this specification in the context of separate embodiments can also be implemented in combination in a single embodiment. Conversely, various features that are described in the context of a single embodiment can also be implemented in multiple embodiments separately or in any suitable sub-combination. Moreover, although features may be described above as acting in certain combinations and even initially claimed as such, one or more features from a claimed combination can in some cases be excised from the combination, and the claimed combination may be directed to a sub-combination or variation of a sub-combination.\|[0106] Similarly, while operations are depicted in the drawings in a particular order, this should not be understood as requiring that such operations be performed in the particular order shown or in sequential order, or that all illustrated operations be performed, to achieve desirable results. In certain circumstances, multitasking and parallel processing may be advantageous. Moreover, the separation of various system components in the embodiments described above should not be understood as requiring such separation in all embodiments, and it should be understood that the described program components and systems can generally be integrated together in a single software product or packaged into multiple software products.\|[0107] Particular embodiments of the subject matter have been described. Other embodiments are within the scope of the following claims. For example, the actions recited in the claims can be performed in a different order and still achieve desirable results. As one example, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In certain implementations, multitasking and parallel processing may be advantageous. Other steps or stages may be provided, or steps or stages may be eliminated, from the described processes. Accordingly, other implementations are within the scope of the following claims.\|Terminology\|[0108] The phraseology and terminology used herein are for the purpose of description and should not be regarded as limiting.\|[0109] The term “approximately”, the phrase “approximately equal to”, and other similar phrases, as used in the specification and the claims (e.g., “X has a value of approximately Y” or “X is approximately equal to Y”), should be understood to mean that one value (X) is within a predetermined range of another value (Y). The predetermined range may be plus or minus 20%, 10%, 5%, 3%, 1%, 0.1%, or less than 0.1%, unless otherwise indicated.\|[0110] The indefinite articles “a” and “an,” as used in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.” The phrase “and/or,” as used in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Multiple elements listed with “and/or” should be construed in the same fashion, i.e., “one or more” of the elements so conjoined. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, a reference to “A and/or B”, when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A only (optionally including elements other than B); in another embodiment, to B only (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc.\|[0111] As used in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of,” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of,” “only one of,” or “exactly one of.” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law.\|[0112] As used in the specification and in the claims, the phrase “at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements. This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase “at least one” refers, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, “at least one of A and B” (or, equivalently, “at least one of A or B,” or, equivalently “at least one of A and/or B”) can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc.\|[0113] The use of “including,” “comprising,” “having,” “containing,” “involving,” and variations thereof, is meant to encompass the items listed thereafter and additional items.\|[0114] Use of ordinal terms such as “first,” “second,” “third,” etc., in the claims to modify a claim element does not by itself connote any priority, precedence, or order of one claim element over another or the temporal order in which acts of a method are performed. Ordinal terms are used merely as labels to distinguish one claim element having a certain name from another element having a same name (but for use of the ordinal term), to distinguish the claim elements.\|[0115] Each numerical value presented herein, for example, in a table, a chart, or a graph, is contemplated to represent a minimum value or a maximum value in a range for a corresponding parameter. Accordingly, when added to the claims, the numerical value provides express support for claiming the range, which may lie above or below the numerical value, in accordance with the teachings herein. Absent inclusion in the claims, each numerical value presented herein is not to be considered limiting in any regard.\|[0116] The terms and expressions employed herein are used as terms and expressions of description and not of limitation, and there is no intention, in the use of such terms and expressions, of excluding any equivalents of the features shown and described or portions thereof. In addition, having described certain embodiments of the invention, it will be apparent to those of ordinary skill in the art that other embodiments incorporating the concepts disclosed herein may be used without departing from the spirit and scope of the invention. The features and functions of the various embodiments may be arranged in various combinations and permutations, and all are considered to be within the scope of the disclosed invention. Accordingly, the described embodiments are to be considered in all respects as only illustrative and not restrictive. Furthermore, the configurations, materials, and dimensions described herein are intended as illustrative and in no way limiting. Similarly, although physical explanations have been provided for explanatory purposes, there is no intent to be bound by any particular theory or mechanism, or to limit the claims in accordance therewith.	Family Number\|(114579754)\|114579754\|Abstract\|(US20250164404 A1)\|A method and system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. In some embodiments, the method includes emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area. The method includes determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target. The method includes converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target. The method also includes analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools. The method further includes providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.\|Title\|(US20250164404 A1)\|System and method for enhanced rock weathering monitoring, reporting, and verification\|Advantages / Prev. Drawbacks\|(US20250164404 A1)\| (...) This technology is particularly useful for assessing the composition of lighter cations relative to heavier cations, aiding in the determination of rock dust weathering status.\|However, measuring the extent and progress of carbon capture is difficult due to the complexity of soil properties and other conditions.\|Independent Claims\|(US20250164404 A1)\| (...) A system for monitoring, reporting, and verification of enhanced rock weathering comprising: (...) provide assessments on carbon dioxide removal and insights on enhanced rock weathering.\| (...) A method for monitoring, reporting, and verification of enhanced rock weathering comprising: (...) providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.\|	Analysis of biological materials	G01N-021/71/8\|G01N-033/24\|G01N-033/24/1\|G01N-033/245\|G01N-2201/0216\|G01N-2201/0221\|G01N-2201/06113\|G01N-2201/12746		G01N-021/71/8\|G01N-033/24\|G01N-033/24/1\|G01N-033/245\|G01N-2201/0216\|G01N-2201/0221\|G01N-2201/06113\|G01N-2201/12746	G01N-021/71\|G01N-033/24	G01N-021/71\|G01N-033/24										PENDING	(US20250164404)\|PENDING	ALIVE	(US20250164404)\|ALIVE	(US20250164404)\|LEGAL DETAILS FOR US20250164404\|Actual or expected expiration date=2044-11-20\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-11-20\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US18954208\|Application date=2024-11-20\|Standardized application number=2024US-18954208\|Event publication date=2024-11-20\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:DOUMBIA, MOHAMED\|Event publication date=2024-11-20\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: IMS-002US\|Event publication date=2024-11-20\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 162143\|Event publication date=2024-11-20\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2024-11-20\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2024-11-20\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=2877\|Event publication date=2024-11-20\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2024-11-20\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2024-11-20\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2024-11-26\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2024-11-29\|Event code=US/POAC\|Event group=Change of name or address\|Change in Power of Attorney (May Include Associate POA)\|Event publication date=2024-11-29\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2024-12-27\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2024-12-27\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-05-22\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250164404\|Publication stage code=A1\|Publication date=2025-05-22\|Standardized publication number=US20250164404\|Event publication date=2025-05-22\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2026-03-22\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner		(US20250164404)\|US	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcOL9D3zefy0h3ePXCJGwxO7JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022751788&ekey=2410&xpn=US20250164404&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/18954208/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=YH%252BWdJIGbNl11gTCkuP4xcRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(US20250164404)\|US	(US20250164404)\|NAME=Impossible Sensing LLC , CITY=St. Louis , STATE=MO , COUNTRY=US NAME=Mati Carbon PBC , CITY=Wilmington , STATE=DE , COUNTRY=US			(US20250164404)\|US; US; US	(US20250164404)\|NAME=Sobron Pablo, CITY=St. Louis, STATE=MO , COUNTRY=US \|NAME=Jordan Jacob S., CITY=St. Louis, STATE=MO , COUNTRY=US \|NAME=Agarwal Shantanu, CITY=Houston, STATE=TX , COUNTRY=US	(US20250164404)\|7	2	1					(US20250164404)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,14\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|	(US20250164404)\|Provisional Appl: US63/601,059 FDD=2023-11-20 [2023US-63601059]	(US20250164404)\|ENGLISH (ENG)	(US20250164404)\|Patent	Titre: (US20250164404)\|System and method for enhanced rock weathering monitoring, reporting, and verification Résumé: (US20250164404)\|A method and system for monitoring, reporting, and verification of enhanced rock weathering is disclosed. In some embodiments, the method includes emitting, using a spectroscopy device, one or more optical signals directed to a target collected from a target area. The method includes determining, using the spectroscopy device, spectral measurements of the optical signals collected from the target. The method includes converting, using a data analysis subsystem, the spectral measurements to data indicating compositional characteristics of the target. The method also includes analyzing, by the data analysis subsystem, the data indicating compositional characteristics of the target using a plurality of analytical tools. The method further includes providing, using the data analysis subsystem, assessments on carbon dioxide removal and insights on enhanced rock weathering.	7	Abstract	gpt-4o-mini	yes	The article focuses on monitoring and verifying enhanced rock weathering, which is directly related to the process of accelerating mineral weathering for CO₂ removal.
5	AU2009900426\|AU2010210311\|WOAU2010/000124	WOAU2010/000124\|HK12105806\|IN6815/DELNP/2011\|EP10738163\|CN201080013080\|AU2010210311	IN6815/DELNP/2011\|HK1164777\|EP2393577\|CN102395417\|EP2393577\|AU2010210311\|WO2010/088738	1878278	WO2010/088738 A1 2010-08-12 [WO201088738]\|HK1164777 A 2012-09-28 [HK1164777]\|IN6815/DELNP/2011 A 2012-12-14 [IN2011DN06815]\|EP2393577 A4 2012-08-01 [EP2393577]\|EP2393577 A1 2011-12-14 [EP2393577]\|CN102395417 A 2012-03-28 [CN102395417]\|AU2010210311 A1 2011-09-01 [AU2010210311]	2009-02-06\|2010-02-08	2010-02-08\|2012-06-14\|2011-09-06\|2010-02-08\|2010-02-08\|2010-02-08	2012-12-14\|2012-09-28\|2012-08-01\|2012-03-28\|2011-12-14\|2011-09-01\|2010-08-12		(EP2393577)\|2014-09-02\|(WO2010/088738)\|2012-08-06\|(CN102395417)\|2014-12-03\|(IN6815/DELNP/2011)\|2022-12-14\|(HK1164777)\|2017-09-28\|(AU2010210311)\|2014-09-04	(EP2393577)\|System, apparatus and method for carbon dioxide sequestration	(EP2393577)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.	HUNWICK RICHARD J ([AU])\|Hunwick Richard J ([AU])\|HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD J. ([AU])\|HUNWICK RICHARD J ([AU])	(EP2393577)\|Hunwick, Richard J. ([AU])\|(EP2393577)\|Hunwick, Richard J. ([AU])\|(WO2010/088738)\|HUNWICK, Richard, J. ([AU])\|(CN102395417)\|HUNWICK RICHARD J. ([AU])\|(IN6815/DELNP/2011)\|HUNWICK RICHARD J ([AU])\|(HK1164777)\|Hunwick Richard J ([AU])\|(AU2010210311)\|Hunwick Richard	HUNWICK RICHARD J	(EP2393577)\|Hunwick, Richard J.\|(EP2393577)\|Hunwick, Richard J.	(EP2393577)\|De Clercq, Ann G. Y.;De Clercq & Partners ([BE])\|Reg. Nb: 101201288\|(WO2010/088738)\|GRIFFITH HACK ([AU])\|(CN102395417)\|LIU JIFU;CHINABLE INTELLECTUAL PROPERTY\|WANG LEI;CHINABLE INTELLECTUAL PROPERTY\|(HK1164777)\|MARKS & CLERK ([HK])\|(AU2010210311)\|Griffith Hack ([AU])	(WO2010/088738)\|A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor.\|It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations.\|The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage).\|However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\|If the quantities of calcium oxide naturally present in fly ash are inadequate, they may, in an embodiment, be augmented by adding pulverised limestone to raw power station flue gases in the boilers at one or more locations for example immediately upstream of the economiser section of the boilers, where flue gas temperatures are appropriate for the decomposition of limestone to calcium oxide and carbon dioxide (when exposed to furnace temperatures of 1,0000C or more, limestone is calcined to quicklime.\|The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s).\|	(WO2010/088738)\|1. A carbon dioxide sequestration process including the steps of:(i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium carbonate that is able to absorb the carbon dioxide, whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate;(ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|24. A system for sequestering carbon dioxide from a gas stream, the system comprising:(a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and(b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|38. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica.\|39. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|44. A method substantially as hereinbefore described with reference to the accompanying drawings.\|45. A system substantially as hereinbefore described with reference to the accompanying drawings.\|	(WO2010/088738)\|In accordance with a second aspect of the present invention there is provided a system for sequestering carbon dioxide from a gas stream, the system comprising: (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and\|Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\|hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica. In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|	(WO2010/088738)\|METHANEDIONE(100,69)\|SLURRY(100,37)\|PIPELINE(100,28)\|SILICATE SLURRY(100,14)\|METAL SILICATE SLURRY(100,13)\|METHANEDIONE SEQUESTRATION(100,11)\|FLOW PATH(100,9)\|GAS STREAM(100,8)\|SEQUESTRATION(100,7)\|CARBON SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|CARBON SEQUESTRATION(100,2)\|AMMONIUM 1 BICARBONATE METAL(100,1)\|BICARBONATE METAL(100,1)\|FLOW PATH PROVISION(100,1)\|REACTIVE AMMONIUM 1 BICARBONATE METAL(100,1)\|HARTSHORN(91,13)\|LIMESTONE PULVERIZATION(91,6)\|METHANEDIONE RICH FLUE GAS(90,2)\|METAL SILICATE(74,37)\|REACTION SLURRY(73,16)\|MAGNESIUM RICH SILICATE(65,8)\|PULVERIZED LIMESTONE INTRODUCTION(63,2)\|METAL CARBONATE(58,10)\|BICARBONATE(56,12)\|REACTOR(52,26)\|METAL SILICATE ROCK(51,3)\|CHESHUNT MIXTURE(48,46)\|REACTION ENHANCEMENT(45,5)\|HARTSHORN SOLUTION(42,3)\|RECOVERED CHESHUNT MIXTURE(40,6)\|MOLECULAR AMMONIA(36,14)\|ABSORBENT SLURRY(34,15)\|RAW FLUE GAS(31,8)\|CHESHUNT MIXTURE SOLUTION(28,10)\|ECONOMIZER SECTION(28,3)\|SILICATE(25,9)\|SEPARATION SYSTEM(24,3)\|THICKENING TANK(23,8)\|INSOLUBLE METAL CARBONATE SILICA(23,2)\|UNDERGROUND CHAMBER(20,8)\|RESIDUAL AMMONIA SCRUBBER(20,4)\|FLUE GAS STREAM(20,1)\|OLIVINE(18,6)\|CARBONATE METAL SILICATE SLURRY(18,3)\|FLUE GAS(17,36)\|RECOVERY SYSTEM(17,3)\|METHANEDIONE PERMANENT SEQUESTRATION(17,1)\|AQUEOUS PHASE(16,23)\|SOLUTION CIRCULATION(16,14)\|CHAMBER PRODUCT(16,2)\|FEEDER(16,2)\|ULTRABASIC MINERAL(16,2)\|MINERAL CARBONATION(15,3)\|PRODUCING CHAMBER(15,2)\|CHILLING PLANT(14,3)\|BICARBONATE NH4HCO(14,2)\|COOL AQUEOUS PHASE(14,2)\|COOLING SYSTEM(14,2)\|HUNTER VALLEY(14,2)\|INCOMING SILICATE SLURRY(14,2)\|INEVITABLE BYPRODUCT(14,2)\|INSOLUBLE MAGNESIA(14,2)\|METAL SILICATE SOLID(14,2)\|METHANEDIONE SINK(14,2)\|MIXED SOLUTION(14,2)\|CHILLED AMMONIATED SLURRY(14,1)\|SULFATE ION(13,5)\|CARBONATED SILICATE SLURRY(13,1)\|METHANEDIONE TONNE(13,1)\|SERPENTINE QUARRY SITE(13,1)\|COAL FIRED POWER STATION(12,6)\|INSOLUBLE CARBONATE(12,3)\|THRESHOLD LEVEL(12,3)\|HOT SILICATE SLURRY(12,2)\|PERMANENT EMPLACEMENT(12,2)\|ULTRAMAFIC MINERAL(12,2)\|THICKENING STAGE(11,3)\|METHANEDIONE CONTENT(11,2)\|BLACK COAL MWE(11,1)\|CARBONATED MINERAL FINAL EMPLACEMENT(11,1)\|CENT METHANEDIONE(11,1)\|SPARINGLY SOLUBLE HYDRATED SALT(11,1)\|AMMONIA LOSS(10,3)\|AMMONIA ABSORPTION CHILLER(10,2)\|FINAL PERMANENT REPOSITORY(10,2)\|FIRED ELECTRICITY GENERATION PLANT(10,2)\|CARBAMATE NH4COONH(10,1)\|CLARIFIED SUPERNATANT(10,1)\|CLARIFIER OVERFLOW(10,1)\|DEINKING ASH(10,1)\|ELECTRICITY GWH(10,1)\|FIN FAN COOLER(10,1)\|GASEOUS METHANEDIONE(10,1)\|INSTALLATION CIRCUMSTANCE(10,1)\|METHANEDIONE FAVOR FORMATION(10,1)\|MINERAL QUARRY SITE(10,1)\|MOLECULAR METHANEDIONE CO2(10,1)\|MULTISTAGE BARREL PUMP(10,1)\|PRESSURIZED METHANEDIONE(10,1)\|QUICKLIME GYPSUM(10,1)\|SERPENTINE MG3SI2O(10,1)\|STACKED SUBCHAMBER(10,1)\|STAGE THICKENER OVERFLOW(10,1)\|TALL SCRUBBING CHAMBER(10,1)\|CARBON DIOXIDE(9,3)\|STATIC HEAD(9,2)\|POWER STATION SITE(8,8)\|SOX(8,7)\|INSOLUBLE SOLID(8,4)\|AMMONIUM HYDROXIDE NH4OH(8,2)\|MINERAL MATTER(8,2)\|PUMPING ENERGY(8,2)\|RETURN PIPELINE(8,2)\|SOLUBLE SALT(8,2)\|SOLUBLE SUBSTANCE(8,2)\|AMMONIA RECOVERY VESSEL(8,1)\|AUSTRALIAN CONTEXT(8,1)\|CIRCULATING SOLUTION DELUGING SPRAY(8,1)\|DENSE SLURRY STREAM(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|INCOMING REACTIVE SLURRY(8,1)\|LIME CALCINATION(8,1)\|LJUNGSTROM ROTARY(8,1)\|MERCURY VAPOR(8,1)\|METHANEDIONE ABSORPTION CHAMBER(8,1)\|METHANEDIONE RICH GAS(8,1)\|MINERAL CARBONATE(8,1)\|PYROXENE MINERAL(8,1)\|PYROXENE SILICATE MINERAL(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|SCRUBBING VESSEL(8,1)\|SLURRY CIRCULATION(8,1)\|THICKENER BALANCE(8,1)\|FLUE GAS FILTER(7,3)\|REACTION CHAMBER(7,3)\|REACTION SOLUTION(7,3)\|ABSORB SURPLUS SENSIBLE HEAT(7,1)\|ALKALINE INDUSTRY RESIDUE(7,1)\|AMMONIA ABSORPTION CHAMBER(7,1)\|AMMONIA MILLION(7,1)\|BOOSTER PUMPING STATION(7,1)\|CHILLING CAPACITY(7,1)\|CIRCULATING SOLUTION ACIDITY(7,1)\|CONCENTRIC PIPE(7,1)\|EMPLACEMENT CONTENT(7,1)\|FINAL THICKENER TANK(7,1)\|FUEL COMBUSTION(7,1)\|GEHO PUMP(7,1)\|HOT SLURRY RISING(7,1)\|INORGANIC COMPONENT(7,1)\|ION EQUILIBRIUM(7,1)\|IRON DISULFIDE FES(7,1)\|KEY CARBONATION REACTION(7,1)\|MINE SITE(7,1)\|MINE VOID(7,1)\|MOLL CO2(7,1)\|NATURAL SILICATE(7,1)\|NONVOLATILE MERCURIC OXIDE(7,1)\|OXIDIZING ENVIRONMENT(7,1)\|PAPER RECYCLING RESIDUE COMBUSTION(7,1)\|PIPELINE REACTOR CHOICE(7,1)\|PRE METHANEDIONE(7,1)\|PRETREATMENT EXTENT(7,1)\|RAW SLURRY(7,1)\|RELEVANT GOVERNMENT(7,1)\|RESIDUAL STREAM CIRCULATION(7,1)\|SCRUBBING ZONE(7,1)\|SPRAY BANK(7,1)\|THICKENER SEPARATION(7,1)\|UNDERGROUND REACTOR PRODUCT(7,1)\|FILTER CAKE(6,5)\|ADJACENT FLOW PATH(6,2)\|FEED STREAM(6,2)\|FILTRATION MEDIUM(6,2)\|NILO2CO(6,2)\|PRECIPITATE(6,2)\|WOLLASTONITE(6,2)\|ABSORPTION ZONE(5,1)\|AMMONIATED SOLUTION(5,1)\|BICARBONATE ION(5,1)\|CARBONATION PRODUCT(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FILTER CLOTH(5,1)\|FINAL REACTION SLURRY(5,1)\|FLUE GAS DESULFURIZATION SCRUBBER(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|IMPURITY GAS(5,1)\|MAGNESIUM ION(5,1)\|METHANEDIONE RATIO(5,1)\|METHANEDIONE SOURCE(5,1)\|MINERAL TRANSPORT(5,1)\|NEXT THICKENER TANK(5,1)\|PIPE REACTOR(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|POWER STATION BOILER ECONOMIZER(5,1)\|POWERFUL OXIDIZING AGENT(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECOMBINATION REACTION(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|REQUISITE EXTENT(5,1)\|SALT DISSOLUTION(5,1)\|SALT HYDRATION(5,1)\|SCRUBBING SOLUTION(5,1)\|SESQUICARBONATE(5,1)\|SLURRY FEED(5,1)\|SOLUTION OFNH4HCO(5,1)\|STRATEGIC LOCATION(5,1)\|STREAM RETURN(5,1)\|SUBSTANCE DISSOLUTION(5,1)\|SULFUR CONTENT(5,1)\|SULFUR DIOXIDE SO2(5,1)\|COUNTER CURRENT DECANTATION(4,15)\|2NH4HCO(4,1)\|6NH4HCO(4,1)\|AGITATION(4,1)\|AIR PREHEATING(4,1)\|ALIGNED CHAMBER(4,1)\|AMMONIA RATIO(4,1)\|AMMONIA RICH NORMAL CARBONATE(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SOLUTION(4,1)\|ANNULUS(4,1)\|AQUEOUS PHASE CENT(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BIOMASS(4,1)\|CARBONATE RICH CHESHUNT MIXTURE(4,1)\|CASO4 2H2O(4,1)\|CHESHUNT MIXTURE SALT(4,1)\|CHILLED SOLUTION(4,1)\|CLEAR OVERFLOW SOLUTION(4,1)\|CONCENTRIC INNER(4,1)\|COOL GAS(4,1)\|COOLING WATER CIRCULATION(4,1)\|CRUSHING(4,1)\|DELUGE(4,1)\|DISCHARGE END(4,1)\|DOLOMITE(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|DRIVING MAGNESIUM(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|EXCESS AQUEOUS PHASE(4,1)\|FLY ASH SOLID(4,1)\|HEADER(4,1)\|HEAT CONSERVATION(4,1)\|HIGHLY EFFICIENT SCRUBBER(4,1)\|HYDROGEN ION CONCOMITANT FORMATION(4,1)\|INDICATIVE MASS BALANCE FIGURE(4,1)\|INORGANIC SOLID(4,1)\|INTERMEDIATE SALT(4,1)\|IRRADIATION(4,1)\|LIDDELL POWER STATION(4,1)\|LIMESTONE(4,1)\|LUMP PRODUCT(4,1)\|MAFIC ROCK(4,1)\|\|(CN102395417)\|CARBON DIOXIDE(100,143)\|SILICATE SLURRY(100,17)\|METAL SILICATE SLURRY(100,15)\|CARBON DIOXIDE SEQUESTRATION(100,14)\|GAS STREAM(100,10)\|CARBON SEQUESTRATION(100,8)\|FLUID CHANNEL(100,8)\|PIPELINE(100,7)\|FLUID PASSAGEWAY(100,5)\|CARBON SEQUESTRATION(100,3)\|PULVERIZED LIMESTONE(100,3)\|AMMONIUM BICARBONATE METAL(100,2)\|BICARBONATE METAL(100,2)\|SEQUESTERING CARBON DIOXIDE(100,2)\|REACTED AMMONIUM BICARBONATE METAL(100,1)\|SLURRY REACTION(100,1)\|METAL SILICATE ROCK(78,11)\|AMMONIUM BICARBONATE(77,27)\|REACTION SLURRY(77,16)\|DEPTH UNDERGROUND(69,1)\|REACTOR(65,32)\|METAL SILICATE(64,36)\|MAGNESIUM RICH SILICATE(59,8)\|METAL CARBONATE(57,14)\|AMMONIUM CARBONATE(56,50)\|PRETREATMENT EXTENT(52,1)\|AMMONIUM BICARBONATE SOLUTION(47,6)\|CARBON DIOXIDE CAPTURE(43,1)\|AMMONIUM CARBONATE SOLUTION(42,20)\|CARBONATE RICH SOLUTION(42,2)\|BICARBONATE(38,9)\|INSOLUBLE CARBONATE(38,4)\|MOLECULAR AMMONIA(37,15)\|ABSORBENT SLURRY(34,15)\|SLURRY(33,37)\|SILICATE(31,9)\|CARBON DIOXIDE CONVERSION(31,1)\|REACTOR CONTROL(31,1)\|WASHING CHAMBER(29,5)\|CARBON DIOXIDE RICH(28,4)\|RAW FLUE GAS(27,9)\|CARBONATE METAL SILICATE SLURRY(26,3)\|RESIDUAL AMMONIA SCRUBBER(23,5)\|INSOLUBLE METAL CARBONATE SILICA(23,2)\|REMOVING CARBON DIOXIDE(23,2)\|FLUE GAS(22,44)\|AMMONIUM CARBONATE SALT SOLUTION(22,7)\|POWER PLANT BOILER(21,5)\|SEQUESTRATION(21,5)\|MINERAL(19,10)\|CALCIUM HYDROXIDE(18,5)\|RETURN CHANNEL(18,4)\|CAVITY PRODUCTION(17,2)\|CHAMBER PRODUCT(17,2)\|FEEDER(17,2)\|AQUEOUS PHASE(16,22)\|SUBTERRANEAN CHAMBER(16,5)\|CARBONATION REACTION(15,4)\|MINERAL CARBONATION(15,3)\|CHILLED AMMONIATED SLURRY(15,1)\|SILICATE ROCK QUARRY(15,1)\|SOLUTION CIRCULATION(14,11)\|COAL FIRED POWER PLANT(14,6)\|UNDERGROUND CHAMBER(14,4)\|000MWE BITUMINOUS COAL(14,2)\|COOL AQUEOUS PHASE(14,2)\|METAL SILICATE SOLID(14,2)\|POWER PLANT(13,30)\|MIXED SOLUTION(13,3)\|HYDROSTATIC HEAD(13,2)\|AMMONIA RICH ORTHOCARBONATE(13,1)\|NONVOLATILE OXIDIZED MERCURY(13,1)\|CRUSHED LIMESTONE(12,2)\|HUNTER VALLEY(12,2)\|ABOVEGROUND PIPELINE(12,1)\|BOILER ECONOMIZER(12,1)\|FIN FAN COOLER(12,1)\|INSOLUBLE CARBONATED MINERAL(12,1)\|MINERAL SILICATESCARBON DIOXIDE(12,1)\|SERPENTINE QUARRY(12,1)\|STAGE CONCENTRATOR OVERFLOW(12,1)\|ULTRABASIC MINERAL(12,1)\|TEMPERATURE SILICATE SLURRY(10,3)\|AMMONIA ABSORPTION CHAMBER(10,2)\|CONCENTRATOR SEPARATION(10,2)\|ABOVEGROUND PIPING(10,1)\|CLARIFIER OVERFLOW(10,1)\|ENERGY THIRSTY TREND(10,1)\|GWH EMISSION(10,1)\|HYDRATED SALT GYPSUM(10,1)\|INCOMING SILICATE SLURRY(10,1)\|INSTALLATION CIRCUMSTANCE(10,1)\|MULTISTAGE CARTRIDGE PUMP(10,1)\|NITRATE ION ACCUMULATION(10,1)\|OLIVINE STONE(10,1)\|PREDOMINANT NATURALLY OCCURRING ADSORBATE(10,1)\|REACTOR SURROUNDINGS(10,1)\|TALL SCRUBBING CHAMBER(10,1)\|ULTRAFERRIERITE MINERAL(10,1)\|INSOLUBLE SOLID(9,4)\|AMMONIA LOSS(9,3)\|AMMONIA RECOVERY VESSEL(9,1)\|AMMONIA RICH AMMONIUM(9,1)\|BURNING BOILER(9,1)\|CONCENTRATOR REST(9,1)\|CONDENSING TOWER(9,1)\|DEINKING ASH(9,1)\|EQUILIBRIUM NITRATE(9,1)\|MAGNESIUM INGRESS(9,1)\|MAGNESIUM ION DISSOLUTION(9,1)\|MINE VOID(9,1)\|MINERAL CARBONATE(9,1)\|PERMANENTLY TREATING INSPECTED GAS(9,1)\|PYROXENE MINERAL(9,1)\|PYROXENE SILICATE MINERAL(9,1)\|SCRUBBING VESSEL(9,1)\|SERPENTINE STONE(9,1)\|SILICATE MINERAL QUARRY(9,1)\|SLURRY CIRCULATION(9,1)\|SPRAYER BANK(9,1)\|ULTRAMAFIC MINERAL(9,1)\|CONCENTRATION TANK(8,2)\|HYDROXIDE ION(8,2)\|PERMANENT PLACEMENT(8,2)\|PUMPING ENERGY(8,2)\|AQUEOUS SOLUTION(7,6)\|FLUE GAS FILTER(7,3)\|PRETREATMENT(7,2)\|SOLUBLE SALT(7,2)\|ALKALINE INDUSTRIAL RESIDUE(7,1)\|AMMONIA ABSORPTION CHILLER(7,1)\|AMMONIA MILLION(7,1)\|AMMONIUM CARBAMATE RICH SOLUTION(7,1)\|AMMONIUM SULFATE QUICKLIME(7,1)\|BURNING PAPER RECYCLING RESIDUE(7,1)\|CHILLING CAPACITY(7,1)\|CIRCULATING SOLUTION ACIDITY(7,1)\|COOLED FILTERED SMOKE(7,1)\|DISSOLVE TARGET(7,1)\|DIVALENT IRON ION(7,1)\|EXTRACTING(7,1)\|GAS XTHE(7,1)\|GEHO PUMP(7,1)\|INCOMING REACTION SLURRY(7,1)\|INORGANIC COMPONENT(7,1)\|INSOLUBLE MAGNESIUM HYDROXIDE PRECIPITATION(7,1)\|NITRATE RADICAL(7,1)\|PIPELINE REACTOR CHOICE(7,1)\|PREDOMINANT SALT(7,1)\|RELEVANT GOVERNMENT(7,1)\|RESIDUAL AMMONIUM SALT(7,1)\|RESIDUAL SOLUBLE SPECIES(7,1)\|SCRUBBING ZONE(7,1)\|SHOWER SPRAY(7,1)\|SIDESTREAM TREATMENT(7,1)\|SILICATE SLURRY FLOW CARBONATION(7,1)\|SPRAY HEADER(7,1)\|STACKED CAVITY(7,1)\|UNDERGROUND REACTOR PRODUCT(7,1)\|XSULFATE ION(7,1)\|FILTER CAKE(6,5)\|CARBON DIOXIDE SEQUESTRATION(6,4)\|CRITICAL LEVEL(6,3)\|ACTIVE SLURRY(6,2)\|CARBON DIOXIDE ABSORPTION CHAMBER(6,2)\|CARBON DIOXIDE EMISSION(6,2)\|ELECTRICITY(6,2)\|TEMPERATURE SLURRY(6,2)\|WOLLASTONITE(6,2)\|XBURNER(6,2)\|XCONVERSION(6,2)\|ABSORB EXCESS(6,1)\|AERATE LARGE SLURRY POND(6,1)\|ALKALI RICH SILICATE(6,1)\|AMMONIA COMPLEX(6,1)\|AMMONIA RICH SOLUTION(6,1)\|AMMONIATED SOLUTION(6,1)\|AMMONIUM BICARBONATE SALT(6,1)\|AMMONIUM SALT CIRCULATING SOLUTION(6,1)\|BICARBONATE ION(6,1)\|BICARBONATE REACTION(6,1)\|BOOSTER PUMP STATION(6,1)\|BYPRODUCT(6,1)\|CARBON DIOXIDE ADSORBATE(6,1)\|CARBONATE AMMONIUM BICARBONATE(6,1)\|CLASSIFICATION(6,1)\|CLEAR SUPERNATANT(6,1)\|CONCENTRIC TUBE(6,1)\|CONTAMINANT GAS(6,1)\|COUNTERCURRENT HEAT EXCHANGER(6,1)\|DENSITY SLURRY STREAM(6,1)\|DISSOLVED SPECIES(6,1)\|FEED GAS(6,1)\|FEED SLURRY(6,1)\|FEEDSTOCK(6,1)\|FILTER CLOTH(6,1)\|FINAL REACTION SLURRY(6,1)\|FLUE GAS DESULFURIZATION SCRUBBER(6,1)\|FRICTION LOSS(6,1)\|GAS INSPECTION(6,1)\|GYPSUM AMMONIUM HYDROXIDE(6,1)\|INSOLUBLE MATTER(6,1)\|MINERAL TRANSPORT(6,1)\|MIXING FLY ASH(6,1)\|NATURAL DRAFT COOLING TOWER(6,1)\|NEXT THICKENING TANK(6,1)\|ORTHOCARBONATE SALT METAL SILICATE SLURRY(6,1)\|OXIDIZING ENVIRONMENT(6,1)\|PREDOMINANT REACTION(6,1)\|PUMPING CAPACITY(6,1)\|RECOMBINATION REACTION(6,1)\|RECUPERATIVE HEAT EXCHANGER(6,1)\|RETURNING STREAM(6,1)\|SCRUBBED FLUE GAS(6,1)\|SESQUICARBONATE(6,1)\|STABLE MINERAL(6,1)\|STRATEGIC LOCATION(6,1)\|SULFUR CONTENT(6,1)\|WET GRINDING(6,1)\|SULFUR OXIDE(5,9)\|FILTRATION(5,3)\|MAGNESIUM CARBONATE(5,3)\|REACTION SOLUTION(5,3)\|UREA(5,3)\|COUNTER CURRENT DECANTATION(4,14)\|ACTIVATED AMMONIUM BICARBONATE METAL(4,1)\|AIR PREHEATING(4,1)\|AMMONIA CONTENT(4,1)\|AMMONIA RATIO(4,1)\|AMMONIA REMAINS(4,1)\|AMMONIA SOLUTION(4,1)\|AMMONIUM CARBONATE SALT RECOVERY(4,1)\|AMMONIUM ORTHOCARBONATE SALT SOLUTION(4,1)\|APPLICABLE EMISSION LIMIT(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWAVE POWER PLANT(4,1)\|BIOMASS(4,1)\|BLAST FURNACE(4,1)\|CARBON DIOXIDE ABSORPTION ZONE(4,1)\|CARBON DIOXIDE TENDENCY(4,1)\|CARBON DIOXIDE TON(4,1)\|CEMENT KILN(4,1)\|CHEMISTRY(4,1)\|CHILLED SOLUTION(4,1)\|COMMINUTION(4,1)\|CONVEYING METAL SILICATE SOLUTION(4,1)\|COOL GAS(4,1)\|COOLING WATER CIRCULATION(4,1)\|DOLOMITE(4,1)\|DOWNSTREAM GAS(4,1)\|ECONOMIZER SECTION(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|\|(IN6815/DELNP/2011)\|METHANEDIONE(100,70)\|SLURRY(100,37)\|PIPELINE(100,28)\|SILICATE SLURRY(100,14)\|METAL SILICATE SLURRY(100,13)\|METHANEDIONE SEQUESTRATION(100,12)\|FLOW PATH(100,9)\|GAS STREAM(100,9)\|SEQUESTRATION(100,8)\|CARBON SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|CARBON SEQUESTRATION(100,2)\|AMMONIUM 1 BICARBONATE METAL(100,1)\|BICARBONATE METAL(100,1)\|FLOW PATH PROVISION(100,1)\|REACTIVE AMMONIUM 1 BICARBONATE METAL(100,1)\|HARTSHORN(66,14)\|LIMESTONE PULVERIZATION(61,6)\|METHANEDIONE RICH FLUE GAS(60,2)\|REACTION SLURRY(54,17)\|METAL SILICATE(52,38)\|MAGNESIUM RICH SILICATE(44,8)\|PULVERIZED LIMESTONE INTRODUCTION(42,2)\|METHANEDIONE CAPTURE(42,1)\|BICARBONATE(41,13)\|METAL CARBONATE(41,11)\|HARTSHORN SOLUTION(38,4)\|REACTOR(37,27)\|CHESHUNT MIXTURE(35,48)\|METAL SILICATE ROCK(34,3)\|REACTION ENHANCEMENT(30,5)\|RECOVERED CHESHUNT MIXTURE(26,6)\|MOLECULAR AMMONIA(24,14)\|ABSORBENT SLURRY(23,15)\|SILICATE(21,10)\|RAW FLUE GAS(21,8)\|ECONOMIZER SECTION(19,3)\|CHESHUNT MIXTURE SOLUTION(18,10)\|SEPARATION SYSTEM(16,3)\|THICKENING TANK(15,8)\|RESIDUAL AMMONIA SCRUBBER(15,5)\|INSOLUBLE METAL CARBONATE SILICA(15,2)\|FLUE GAS STREAM(14,1)\|UNDERGROUND CHAMBER(13,8)\|OLIVINE(12,6)\|CARBONATE METAL SILICATE SLURRY(12,3)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|FLUE GAS(11,36)\|SOLUTION CIRCULATION(11,14)\|RECOVERY SYSTEM(11,3)\|CHAMBER PRODUCT(11,2)\|FEEDER(11,2)\|ULTRABASIC MINERAL(11,2)\|AQUEOUS PHASE(10,23)\|MINERAL CARBONATION(10,3)\|PRODUCING CHAMBER(10,2)\|CHILLED AMMONIATED SLURRY(10,1)\|CHILLING PLANT(9,3)\|BICARBONATE NH4HCO(9,2)\|COOL AQUEOUS PHASE(9,2)\|COOLING SYSTEM(9,2)\|HUNTER VALLEY(9,2)\|INCOMING SILICATE SLURRY(9,2)\|INEVITABLE BYPRODUCT(9,2)\|INSOLUBLE MAGNESIA(9,2)\|METAL SILICATE SOLID(9,2)\|METHANEDIONE SINK(9,2)\|MIXED SOLUTION(9,2)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|SERPENTINE QUARRY SITE(9,1)\|COAL FIRED POWER STATION(8,6)\|SULFATE ION(8,5)\|INSOLUBLE CARBONATE(8,3)\|THRESHOLD LEVEL(8,3)\|HOT SILICATE SLURRY(8,2)\|PERMANENT EMPLACEMENT(8,2)\|ULTRAMAFIC MINERAL(8,2)\|BLACK COAL MWE(8,1)\|CARBONATED MINERAL FINAL EMPLACEMENT(8,1)\|CENT METHANEDIONE(8,1)\|SPARINGLY SOLUBLE HYDRATED SALT(8,1)\|THICKENING STAGE(7,3)\|AMMONIA ABSORPTION CHILLER(7,2)\|FINAL PERMANENT REPOSITORY(7,2)\|FIRED ELECTRICITY GENERATION PLANT(7,2)\|METHANEDIONE CONTENT(7,2)\|CARBAMATE NH4COONH(7,1)\|CLARIFIED SUPERNATANT(7,1)\|CLARIFIER OVERFLOW(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|GASEOUS METHANEDIONE(7,1)\|INSTALLATION CIRCUMSTANCE(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|METHANEDIONE FAVOR FORMATION(7,1)\|MINERAL QUARRY SITE(7,1)\|MOLECULAR METHANEDIONE CO2(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|PRESSURIZED METHANEDIONE(7,1)\|QUICKLIME GYPSUM(7,1)\|SERPENTINE MG3SI2O(7,1)\|STACKED SUBCHAMBER(7,1)\|STAGE THICKENER OVERFLOW(7,1)\|TALL SCRUBBING CHAMBER(7,1)\|INSOLUBLE SOLID(6,4)\|AMMONIA LOSS(6,3)\|CARBON DIOXIDE(6,3)\|STATIC HEAD(6,2)\|AMMONIA RECOVERY VESSEL(6,1)\|AUSTRALIAN CONTEXT(6,1)\|CIRCULATING SOLUTION DELUGING SPRAY(6,1)\|DENSE SLURRY STREAM(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|INCOMING REACTIVE SLURRY(6,1)\|LIME CALCINATION(6,1)\|LJUNGSTROM ROTARY(6,1)\|MERCURY VAPOR(6,1)\|METHANEDIONE ABSORPTION CHAMBER(6,1)\|METHANEDIONE RICH GAS(6,1)\|MINERAL CARBONATE(6,1)\|PYROXENE MINERAL(6,1)\|PYROXENE SILICATE MINERAL(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|SCRUBBING VESSEL(6,1)\|SLURRY CIRCULATION(6,1)\|THICKENER BALANCE(6,1)\|POWER STATION SITE(5,8)\|SOX(5,7)\|FLUE GAS FILTER(5,3)\|REACTION CHAMBER(5,3)\|REACTION SOLUTION(5,3)\|AMMONIUM HYDROXIDE NH4OH(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|RETURN PIPELINE(5,2)\|SOLUBLE SALT(5,2)\|SOLUBLE SUBSTANCE(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA ABSORPTION CHAMBER(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CHILLING CAPACITY(5,1)\|CIRCULATING SOLUTION ACIDITY(5,1)\|CONCENTRIC PIPE(5,1)\|EMPLACEMENT CONTENT(5,1)\|FINAL THICKENER TANK(5,1)\|FUEL COMBUSTION(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|ION EQUILIBRIUM(5,1)\|IRON DISULFIDE FES(5,1)\|KEY CARBONATION REACTION(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|MOLL CO2(5,1)\|NATURAL SILICATE(5,1)\|NONVOLATILE MERCURIC OXIDE(5,1)\|OXIDIZING ENVIRONMENT(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRE METHANEDIONE(5,1)\|PRETREATMENT EXTENT(5,1)\|RAW SLURRY(5,1)\|RELEVANT GOVERNMENT(5,1)\|RESIDUAL STREAM CIRCULATION(5,1)\|SCRUBBING ZONE(5,1)\|SPRAY BANK(5,1)\|THICKENER SEPARATION(5,1)\|UNDERGROUND REACTOR PRODUCT(5,1)\|FILTER CAKE(4,5)\|ADJACENT FLOW PATH(4,2)\|FEED STREAM(4,2)\|FILTRATION MEDIUM(4,2)\|NILO2CO(4,2)\|PRECIPITATE(4,2)\|WOLLASTONITE(4,2)\|AMMONIATED SOLUTION(4,1)\|BICARBONATE ION(4,1)\|CARBONATION PRODUCT(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FILTER CLOTH(4,1)\|FINAL REACTION SLURRY(4,1)\|FLUE GAS DESULFURIZATION SCRUBBER(4,1)\|GAS TONNE(4,1)\|GEOLOGICAL CONDITION(4,1)\|IMPURITY GAS(4,1)\|MAGNESIUM ION(4,1)\|METHANEDIONE RATIO(4,1)\|METHANEDIONE SOURCE(4,1)\|MINERAL TRANSPORT(4,1)\|NEXT THICKENER TANK(4,1)\|PIPE REACTOR(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|POWER STATION BOILER ECONOMIZER(4,1)\|POWERFUL OXIDIZING AGENT(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECOMBINATION REACTION(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|REQUISITE EXTENT(4,1)\|SALT DISSOLUTION(4,1)\|SALT HYDRATION(4,1)\|SCRUBBING SOLUTION(4,1)\|SESQUICARBONATE(4,1)\|SLURRY FEED(4,1)\|SOLUTION OFNH4HCO(4,1)\|STRATEGIC LOCATION(4,1)\|STREAM RETURN(4,1)\|SUBSTANCE DISSOLUTION(4,1)\|SULFUR CONTENT(4,1)\|SULFUR DIOXIDE SO2(4,1)\|COUNTER CURRENT DECANTATION(3,15)\|2NH4HCO(3,1)\|6NH4HCO(3,1)\|AGITATION(3,1)\|AIR PREHEATING(3,1)\|ALIGNED CHAMBER(3,1)\|AMMONIA RATIO(3,1)\|AMMONIA RICH NORMAL CARBONATE(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|AQUEOUS PHASE CENT(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|CARBONATE RICH CHESHUNT MIXTURE(3,1)\|CASO4 2H2O(3,1)\|CHESHUNT MIXTURE SALT(3,1)\|CHILLED SOLUTION(3,1)\|CLEAR OVERFLOW SOLUTION(3,1)\|CONCENTRIC INNER(3,1)\|COOL GAS(3,1)\|COOLING WATER CIRCULATION(3,1)\|CRUSHING(3,1)\|DELUGE(3,1)\|DISCHARGE END(3,1)\|DOLOMITE(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|DRIVING MAGNESIUM(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|EXCESS AQUEOUS PHASE(3,1)\|FLY ASH SOLID(3,1)\|HEADER(3,1)\|HEAT CONSERVATION(3,1)\|HIGHLY EFFICIENT SCRUBBER(3,1)\|HYDROGEN ION CONCOMITANT FORMATION(3,1)\|INDICATIVE MASS BALANCE FIGURE(3,1)\|INORGANIC SOLID(3,1)\|INTERMEDIATE SALT(3,1)\|IRRADIATION(3,1)\|LIDDELL POWER STATION(3,1)\|LIMESTONE(3,1)\|LUMP PRODUCT(3,1)\|MAFIC ROCK(3,1)\|\|(AU2010210311)\|METHANEDIONE(100,65)\|SLURRY(100,37)\|METHANEDIONE SEQUESTRATION(100,10)\|GAS STREAM(100,6)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,3)\|HARTSHORN(90,13)\|LIMESTONE PULVERIZATION(83,6)\|METHANEDIONE RICH FLUE GAS(81,2)\|REACTION SLURRY(75,14)\|METAL SILICATE(69,33)\|MAGNESIUM RICH SILICATE(59,8)\|PULVERIZED LIMESTONE INTRODUCTION(57,2)\|METAL CARBONATE(56,9)\|HARTSHORN SOLUTION(56,3)\|METHANEDIONE CAPTURE(56,1)\|BICARBONATE(52,12)\|REACTOR(51,24)\|CHESHUNT MIXTURE(48,43)\|METAL SILICATE ROCK(46,3)\|REACTION ENHANCEMENT(41,5)\|RECOVERED CHESHUNT MIXTURE(36,6)\|MOLECULAR AMMONIA(33,14)\|ABSORBENT SLURRY(30,15)\|SILICATE(30,8)\|RAW FLUE GAS(28,8)\|CHESHUNT MIXTURE SOLUTION(26,9)\|ECONOMIZER SECTION(25,3)\|RESIDUAL AMMONIA SCRUBBER(21,5)\|SEPARATION SYSTEM(21,3)\|THICKENING TANK(20,8)\|INSOLUBLE METAL CARBONATE SILICA(20,2)\|BICARBONATE METAL(20,1)\|UNDERGROUND CHAMBER(18,8)\|CARBONATE METAL SILICATE SLURRY(18,2)\|FLUE GAS STREAM(18,1)\|OLIVINE(17,6)\|LAGGED ABOVEGROUND PIPELINE(17,1)\|METHANEDIONE PERMANENT SEQUESTRATION(16,1)\|RECOVERY SYSTEM(15,3)\|CHAMBER PRODUCT(15,2)\|FEEDER(15,2)\|ULTRABASIC MINERAL(15,2)\|AQUEOUS PHASE(14,22)\|SOLUTION CIRCULATION(14,13)\|MINERAL CARBONATION(14,3)\|PRODUCING CHAMBER(14,2)\|CHILLING PLANT(13,3)\|BICARBONATE NH4HCO(13,2)\|COOL AQUEOUS PHASE(13,2)\|COOLING SYSTEM(13,2)\|HUNTER VALLEY(13,2)\|INCOMING SILICATE SLURRY(13,2)\|INEVITABLE BYPRODUCT(13,2)\|INSOLUBLE MAGNESIA(13,2)\|METAL SILICATE SOLID(13,2)\|METHANEDIONE SINK(13,2)\|MIXED SOLUTION(13,2)\|CHILLED AMMONIATED SLURRY(13,1)\|SULFATE ION(12,5)\|CARBONATED SILICATE SLURRY(12,1)\|METHANEDIONE TONNE(12,1)\|SERPENTINE QUARRY SITE(12,1)\|INSOLUBLE CARBONATE(11,3)\|THRESHOLD LEVEL(11,3)\|HOT SILICATE SLURRY(11,2)\|PERMANENT EMPLACEMENT(11,2)\|ULTRAMAFIC MINERAL(11,2)\|THICKENING STAGE(10,3)\|METHANEDIONE CONTENT(10,2)\|CARBONATED MINERAL FINAL EMPLACEMENT(10,1)\|CENT METHANEDIONE(10,1)\|SPARINGLY SOLUBLE HYDRATED SALT(10,1)\|AMMONIA LOSS(9,3)\|AMMONIA ABSORPTION CHILLER(9,2)\|FINAL PERMANENT REPOSITORY(9,2)\|CARBAMATE NH4COONH(9,1)\|CLARIFIED SUPERNATANT(9,1)\|CLARIFIER OVERFLOW(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|FIN FAN COOLER(9,1)\|GASEOUS METHANEDIONE(9,1)\|ID MOLL CO2(9,1)\|INSTALLATION CIRCUMSTANCE(9,1)\|METHANEDIONE ABSORPTION ZONE(9,1)\|METHANEDIONE FAVOR FORMATION(9,1)\|METHANEDIONE ISOLATION(9,1)\|MINERAL QUARRY SITE(9,1)\|MOLECULAR METHANEDIONE CO2(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|QUICKLIME GYPSUM(9,1)\|STACKED SUBCHAMBER(9,1)\|STAGE THICKENER OVERFLOW(9,1)\|TALL SCRUBBING CHAMBER(9,1)\|INSOLUBLE SOLID(8,4)\|CARBON DIOXIDE(8,3)\|CARBON SEQUESTRATION(8,2)\|STATIC HEAD(8,2)\|AMMONIA RECOVERY VESSEL(8,1)\|AUSTRALIAN CONTEXT(8,1)\|CIRCULATING SOLUTION DELUGING SPRAY(8,1)\|DENSE SLURRY STREAM(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|H2O 2NH4HCO(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|INCOMING REACTIVE SLURRY(8,1)\|LIME CALCINATION(8,1)\|LJUNGSTROM ROTARY(8,1)\|MERCURY VAPOR(8,1)\|METHANEDIONE ABSORPTION CHAMBER(8,1)\|METHANEDIONE RICH GAS(8,1)\|MINERAL CARBONATE(8,1)\|PYROXENE MINERAL(8,1)\|PYROXENE SILICATE MINERAL(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|SCRUBBING VESSEL(8,1)\|SLURRY CIRCULATION(8,1)\|THICKENER BALANCE(8,1)\|POWER STATION SITE(7,8)\|SOX(7,7)\|COAL FIRED POWER STATION(7,5)\|FLUE GAS FILTER(7,3)\|MG3SI2O(7,3)\|REACTION CHAMBER(7,3)\|REACTION SOLUTION(7,3)\|AMMONIUM HYDROXIDE NH4OH(7,2)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|RETURN PIPELINE(7,2)\|SOLUBLE SALT(7,2)\|SOLUBLE SUBSTANCE(7,2)\|FILTER CAKE(6,5)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA ABSORPTION CHAMBER(6,1)\|AMMONIA MILLION(6,1)\|BOOSTER PUMPING STATION(6,1)\|CHILLING CAPACITY(6,1)\|CIRCULATING SOLUTION ACIDITY(6,1)\|CONCENTRIC PIPE(6,1)\|EMPLACEMENT CONTENT(6,1)\|FINAL THICKENER TANK(6,1)\|FIRED ELECTRICITY GENERATION PLANT(6,1)\|FUEL COMBUSTION(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INORGANIC COMPONENT(6,1)\|ION EQUILIBRIUM(6,1)\|IRON DISULFIDE FES(6,1)\|KEY CARBONATION REACTION(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|MON CO2(6,1)\|NATURAL SILICATE(6,1)\|NONVOLATILE MERCURIC OXIDE(6,1)\|OXIDIZING ENVIRONMENT(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRE METHANEDIONE(6,1)\|PRETREATMENT EXTENT(6,1)\|RAW SLURRY(6,1)\|RELEVANT GOVERNMENT(6,1)\|RESIDUAL STREAM CIRCULATION(6,1)\|SCRUBBING ZONE(6,1)\|SPRAY BANK(6,1)\|THICKENER SEPARATION(6,1)\|UNDERGROUND REACTOR PRODUCT(6,1)\|6NH4HCO(5,2)\|ADJACENT FLOW PATH(5,2)\|FEED STREAM(5,2)\|FILTRATION MEDIUM(5,2)\|LIMESTONE(5,2)\|PRECIPITATE(5,2)\|WOLLASTONITE(5,2)\|AMMONIATED SOLUTION(5,1)\|BICARBONATE ION(5,1)\|CARBONATION PRODUCT(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COUNTERCURRENT DECANTATION(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FILTER CLOTH(5,1)\|FINAL REACTION SLURRY(5,1)\|FLUE GAS DESULFURIZATION SCRUBBER(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|IMPURITY GAS(5,1)\|MAGNESIUM ION(5,1)\|METHANEDIONE RATIO(5,1)\|METHANEDIONE SOURCE(5,1)\|MINERAL TRANSPORT(5,1)\|NE4HCO SOLUTION(5,1)\|NEXT THICKENER TANK(5,1)\|PIPE REACTOR(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|POWER STATION BOILER ECONOMIZER(5,1)\|POWERFUL OXIDIZING AGENT(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECOMBINATION REACTION(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|REQUISITE EXTENT(5,1)\|SALT DISSOLUTION(5,1)\|SALT HYDRATION(5,1)\|SCRUBBING SOLUTION(5,1)\|SESQUICARBONATE(5,1)\|SLURRY FEED(5,1)\|STABLE MINERAL(5,1)\|STRATEGIC LOCATION(5,1)\|STREAM RETURN(5,1)\|SUBSTANCE DISSOLUTION(5,1)\|SULFUR CONTENT(5,1)\|SULFUR DIOXIDE SO2(5,1)\|SHELL(4,2)\|AGITATION(4,1)\|AIR PREHEATING(4,1)\|ALIGNED CHAMBER(4,1)\|AMMONIA RATIO(4,1)\|AMMONIA RICH NORMAL CARBONATE(4,1)\|ANNULUS(4,1)\|AQUEOUS PHASE CENT(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BIOMASS(4,1)\|CARBONATE RICH CHESHUNT MIXTURE(4,1)\|CLEAR OVERFLOW SOLUTION(4,1)\|CONCENTRIC INNER(4,1)\|COOL GAS(4,1)\|COOLING WATER CIRCULATION(4,1)\|CRUSHING(4,1)\|DELUGE(4,1)\|DISCHARGE END(4,1)\|DOLOMITE(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|DRIVING MAGNESIUM(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|EXCESS AQUEOUS PHASE(4,1)\|FLY ASH SOLID(4,1)\|FURNACE TEMPERATURE(4,1)\|HEADER(4,1)\|HEAT CONSERVATION(4,1)\|HIGHLY EFFICIENT SCRUBBER(4,1)\|HYDROGEN ION CONCOMITANT FORMATION(4,1)\|INDICATIVE MASS BALANCE FIGURE(4,1)\|INORGANIC SOLID(4,1)\|INTERMEDIATE SALT(4,1)\|IRRADIATION(4,1)\|LIDDELL POWER STATION(4,1)\|LUMP PRODUCT(4,1)\|	(WO2010/088738)\|Claims:\|1. A carbon dioxide sequestration process including the steps of:\|(i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium carbonate that is able to absorb the carbon dioxide, whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate;\|(ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|2. A process in accordance with claim 1, wherein the metal silicate rock is mixed the normal ammonium carbonate solution prior to absorbing the carbon dioxide in step\|3. A process in accordance with claim 1 or claim 2, wherein the reaction causes the bicarbonate in the presence of the metal silicate to partially decompose so as to produce an aqueous phase enriched in molecular ammonia and carbon dioxide.\|4. A process in accordance with claim 3, comprising the further step of cooling the aqueous phase such that free ammonia and carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered for re-use in step (i) of the process.\|5. A process in accordance with claim 4, comprising the further step of adding an alkali to the recovered ammonium carbonate in solution prior to being re-used in step (i).\|6. A process in accordance with claim 5, wherein the alkali is calcium oxide and/or hydroxide.\|7. A process in accordance with claim 6, wherein the calcium oxide is extracted from a flue gas stream prior to scrubbing in step (i).\|8. A process in accordance with any one of the preceding claims, comprising the further step of introducing pulverised limestone into a source producing the carbon- dioxide rich flue gasses.\|9. A process in accordance with claim 8, wherein the source is a coal-fired power station boiler and wherein the pulverised limestone is added upstream of an economiser section of the power station boiler.\|10. A process in accordance with claim 2, wherein a portion of the mixed solution used to scrub the gas stream prior to discharge to the atmosphere is chilled to ensure that a quantity of free ammonia in the gases is below a threshold level.\|11. A process in accordance with any one of the preceding claims, wherein the step of scrubbing the gas stream comprises exposing the carbon dioxide-containing gas stream to the solution as a spray.\|12. A process in accordance with any one of the preceding claims, wherein the step of controlling the reactor comprises elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\|13. A process in accordance with any one of the preceding claims, wherein the reactor is a pipeline.\|14. A process in accordance with claim 13, wherein the pipeline comprises multiple flow paths and wherein the reaction takes place along the length of one of the flow paths.\|15. A process in accordance with claim 14, wherein another of the flow paths is utilised to supply the metal silicate slurry to the first stage.\|16. A process in accordance with claim 15, comprising the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\|17. A process in accordance with any one of claims 1 to 12, wherein the reactor is a chamber located in use underground.\|18. A process in accordance with claim 17, wherein the chamber is located at a depth that provides sufficient pressure by way of static head to enhance the reaction between the carbon dioxide and the metal silicate.\|19. A process in accordance with any one of the preceding claims, comprising the further step of grinding a metal silicate rock to produce the metal silicate slurry.\|20. A process in accordance with claim 19, wherein the metal silicate slurry comprises approximately 25% by weight finely ground metal silicate solids.\|21. A process in accordance with any one of the preceding claims, wherein the metal silicate is a magnesium-rich silicate.\|22. A process in accordance with claim 21, wherein the magnesium rich silicate is a serpentine and/or olivine and/or pyroxene.\|23. A process in accordance with any of the preceding claims, comprising the further step of cooling the normal ammonium carbonate-metal silicate slurry prior to scrubbing.\|24. A system for sequestering carbon dioxide from a gas stream, the system comprising:\|(a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide\|reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and\|(b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|25. A system in accordance with claim 23, wherein the reactor is the pipeline as defined in any one of claims 13 to 16.\|26. A system in accordance with claim 23, wherein the reactor is the chamber as defined in any one of claims 17 or 18.\|27. A system in accordance with any one of claims 24 to 26, wherein the first apparatus comprises an absorption chamber arranged to circulate the normal ammonium carbonate solution through the carbon dioxide to thereby absorb the carbon dioxide.\|28. A system in accordance with any one of claims 24 to 27, wherein the reaction of the bicarbonate with the metal silicate further produces an aqueous phase containing molecular ammonia, carbon dioxide and water.\|29. A system in accordance with claim 28, further comprising a cooling arrangement arranged to cool the aqueous phase such that free ammonia and remaining carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered by a recovery arrangement of the system for re-use by the first apparatus.\|30. A system in accordance with claim 29, further comprising a control arrangement arranged to add a controlled amount of alkali to the recovered ammonium carbonate in solution prior to returning it to the first apparatus for re-use.\|31. A system in accordance with claim 29 or 30, further comprising a separation arrangement arranged to separate the recovered ammonium carbonate in solution from the insoluble metal carbonate-silica phase prior to recovery.\|32. A system in accordance with claim 31, wherein the separation arrangement comprises a counter-current decantation (CCD) system.\|33. A system in accordance with any one of claims 30 to 32, wherein the alkali is calcium oxide and/or hydroxide.\|34. A system in accordance with claim 33, wherein the calcium oxide is extracted from the raw flue gas stream prior to scrubbing.\|35. A system in accordance with any one of the preceding claims 24 to 34, comprising a feeder arranged to feed pulverised limestone at a source producing the carbon-dioxide rich flue gasses.\|36. A system in accordance with claim 35, wherein the point source is a coal-fired power station boiler and wherein the pulverised limestone is fed into raw flue gasses upstream of an economiser section of the power station boiler.\|37. A system in accordance with any one of claims 24 to 36, wherein the metal silicate comprises a magnesium rich silicate as defined in any one of claims 21 or 22.\|38. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica.\|39. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of:\|positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|40. A method in accordance with claim 39, wherein the slurry provided to the chamber is the reactive slurry produced in the process of any one of claims 1 to 12, or 19 to 22, when dependent on any one of claims 1 to 4.\|41. A method in accordance with claims 39 or 40, comprising the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber.\|42. A method in accordance with claim 41, wherein the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.\|43. A power station utilising a carbon sequestration system in accordance with any one of claims 24 to 37, the system arranged to sequester carbon dioxide from flue gas emitted by the power station.\|44. A method substantially as hereinbefore described with reference to the accompanying drawings.\|45. A system substantially as hereinbefore described with reference to the accompanying drawings.	(WO2010/088738)\|[0001] SYSTEM, APPARATUS AND METHOD FOR CARBON DIOXIDE\| [0002] SEQUESTRATION\| [0003] Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\| [0004] Background to the Invention\| [0005] There is increased focus on reducing carbon dioxide emissions to the atmosphere, to help minimise the effects of global warming. Carbon dioxide sinks exist naturally, with the main naturally occurring sink being the ocean. Plants are also an effective form of carbon dioxide sink and use photosynthesis to remove carbon from the atmosphere by incorporating it into biomass. However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\| [0006] A major source of harmful carbon dioxide gases are large fossil fuel power stations which, when fuelled by black coal, on average typically output around 0.8 to one tonne of the gas for each MegaWatt-hour (MWh) of electricity they generate. For example, a large power station such as the 2,640 MW Bayswater in the Hunter Valley of New South Wales, Australia, in generating 20 million MWh of electricity in a year, would also output 18 million tonnes of carbon dioxide. It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations. It would also be advantageous if a system and method were provided for the disposition of the gas to be independently audited in perpetuity.\| [0007] Summary of the Invention hi a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| [0008] (i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium carbonate that is able to absorb the carbon dioxide, whereby thecarbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate;\| [0009] (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| [0010] In the context of the present specification, the phrase "solution rich in normal ammonium carbonate " will be understood as referring to a solution whereby the main salt present corresponds to the formula for the normal form of ammonium carbonate\| [0011] (NILO2CO3.. There solution may, however, consist of other ammonium carbonate salts, and there may also be some molecular ammonia NH3, and ammonium hydroxide NH4OH, also present. Further, it should be noted that the terminology "gas stream containing carbon dioxide" does not mean that the stream contains only carbon dioxide, and may contain other off gases.\| [0012] hi an embodiment the metal silicate rock is mixed with the normal ammonium carbonate solution prior to absorbing the carbon dioxide in step (i).\| [0013] hi an embodiment the reaction causes the bicarbonate in the presence of the metal silicate to partially decompose so as to produce an aqueous phase enriched in molecular ammonia and carbon dioxide.\| [0014] hi an embodiment the method comprises the further step of cooling the aqueous phase such that free ammonia and carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered for re-use in step (i) of the process.\| [0015] hi an embodiment the method comprises the further step of adding an alkali to the recovered ammonium carbonate in solution prior to being re-used in step (i). The alkali may be calcium oxide and/or hydroxide, hi an embodiment the calcium oxide is extracted from gas stream prior to scrubbing in step (i).In an embodiment the method comprises the further step of introducing pulverised limestone into a source producing the carbon-dioxide rich gasses. The source may be a coal-fired power station boiler and the pulverised limestone is added upstream of an economiser section of the power station boiler.\| [0016] In an embodiment a portion of the mixed solution used to scrub the gas stream prior to discharge to the atmosphere is chilled to ensure that a quantity of free ammonia in the gases is below a threshold level. The threshold level may, for example, be set by the relevant government or other regulatory body.\| [0017] In an embodiment the step of scrubbing the gas stream comprises exposing the carbon dioxide-containing gas stream to the slurry as a spray or deluge operable to maximise the area of exposure between the slurry and the carbon dioxide-containing gas.\| [0018] In an embodiment the step of controlling the reactor comprises elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\| [0019] In an embodiment the reactor is a pipeline. The pipeline may comprise multiple flow paths and wherein the reaction takes place along the length of one of the flow paths. Another of the flow paths is utilised to supply the metal silicate slurry to the first stage.\| [0020] In an embodiment the method comprises the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\| [0021] In an embodiment the reactor is a chamber located in use underground. The chamber may be located at a depth that provides sufficient pressure by way of static head to enhance the reaction between the carbon dioxide and the metal silicate.In an embodiment the method comprises the further step of grinding a metal silicate rock to produce the metal silicate slurry. The metal silicate slurry may comprise roughly 25% by weight finely ground metal silicate solids.\| [0022] In an embodiment the metal silicate is a magnesium-rich silicate. In an embodiment the magnesium rich silicate is a serpentine and/or olivine and/or pyroxene mineral all commonly described as ultrabasic or ultramafic minerals.\| [0023] In an embodiment the method comprises the further step of cooling the normal ammonium carbonate-metal silicate slurry prior to it use in scrubbing carbon dioxide from flue gases.\| [0024] In accordance with a second aspect of the present invention there is provided a system for sequestering carbon dioxide from a gas stream, the system comprising: (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and\| [0025] (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\| [0026] In an embodiment the first apparatus comprises an absorption chamber arranged to circulate the normal ammonium carbonate solution through the carbon dioxide to thereby absorb the carbon dioxide.\| [0027] hi an embodiment the reactor is the pipeline as used in the method according to the first aspect.\| [0028] In an embodiment the reactor is the chamber used in the method according to the first aspect.In an embodiment the reaction of the bicarbonate with the metal silicate further produces an aqueous phase containing molecular ammonia, carbon dioxide and water.\| [0029] In an embodiment the system further comprises a cooling arrangement arranged to cool the aqueous phase such that free ammonia and remaining carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered by a recovery arrangement for reuse by the first apparatus.\| [0030] In an embodiment the system further comprises a separation system arranged to separate the recovered ammonium carbonate in solution from the insoluble metal carbonate-silica phase prior to recovery. The separation arrangement may, for example, be a counter-current decantation (CCD) system comprising one or more stages for separating the solution.\| [0031] In an embodiment the system further comprises a control arrangement arranged to add an alkali to the recovered ammonium carbonate in solution prior to returning it to the first apparatus for re-use.\| [0032] In an embodiment the alkali is calcium oxide and/or hydroxide. The calcium oxide is extracted along with other suspended solids (fly ash solids) from the gas stream prior to scrubbing.\| [0033] In an embodiment the system further comprises a feeder arranged to feed pulverised limestone into a source producing the carbon-dioxide rich flue gases. The point source may, for example, be a coal-fired power station and the pulverised limestone is fed into raw flue gases upstream of the power station boiler's economiser.\| [0034] In an embodiment the metal silicate comprises a magnesium rich silicate as used in the method according to the first aspect.In an embodiment the system further comprises an ammonium carbonate salt recovery arrangement arranged to recover ammonia and ammonium salts accompanying the final product.\| [0035] In an embodiment, the system comprises a solids-liquids separation system arranged to separate and recover ammonium carbonate salts, from the metal carbonate solid product that is sent for final emplacement.\| [0036] hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica.\| [0037] In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\| [0038] In an embodiment the slurry provided to the chamber is the reactive slurry produced in the process of the first aspect.\| [0039] In an embodiment the method comprises the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber.\| [0040] In an embodiment the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.In accordance with a fifth aspect there is provided a power station or other point source of carbon dioxide-rich flue gases, such as a blast furnace as used in steel making, or a cement kiln, utilising a carbon sequestration system in accordance with the second aspect, the system arranged to capture and sequester carbon dioxide from flue gas emitted by the power station or other point source.\| [0041] In accordance with a sixth aspect, in an ammonia absorption process in which a metal silicate rock is mixed with a normal ammonium carbonate salt solution in water so as to produce a normal ammonium carbonate salt solution in water/metal silicate slurry (the ammoniated slurry) for use in a carbon dioxide sequestration process, there is provided the step of chilling the ammoniated slurry to limit losses of ammonia in scrubbed flue gases to the extent necessary to meet emission limits applying at the location in question.\| [0042] hi an embodiment, the process comprises the further step of providing the ammoniated slurry to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammoniated slurry to thereby absorb the carbon dioxide into a reactive slurry.\| [0043] In accordance with a seventh aspect of the present invention there is provided a method of extracting a target metal from a metal silicate comprising the step of mixing the metal silicate with an ammonia-rich ammonium carbonate salt solution, and reacting the mixed solution to cause the target metal to dissolve into the solution.\| [0044] In an embodiment the method comprises the further step of grinding the metal silicate and forming it into a slurry prior to mixing the metal silicate with the solution.\| [0045] In an embodiment the metal silicate is a magnesium-rich silicate.\| [0046] hi an embodiment the magnesium-rich silicate is a serpentine and/or olivine and/or pyroxene silicate mineral commonly described as an ultrabasic or ultramafic mineral.In an embodiment the solution comprises normal ammonium carbonate salts dissolved in water (the ammoniated solution).\| [0047] In an embodiment the target metal dissolves into the solution and then precipitates in the presence of carbon dioxide, as a metal carbonate to be removed for recovery.\| [0048] In an embodiment the target metal is one or more of magnesium, calcium or iron. The dominant metal within the metal silicate may comprise magnesium.\| [0049] In an eighth aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| [0050] (i) in a first stage, mixing a slurry of a metal silicate rock with a normal ammonium carbonate solution so as to produce a normal ammonium carbonate salt/water/metal silicate slurry;\| [0051] (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the chilled solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| [0052] (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\| [0053] Brief Description of the Drawings\| [0054] An embodiment of the present invention will now be described, by way of example only, with reference to the accompanying drawings, in which:\| [0055] Fig. 1 is a schematic of a carbon dioxide sequestration system according to an embodiment of the present invention;\| [0056] Fig. 2 is a schematic of a carbon dioxide sequestration system according to an alternative embodiment of the present invention;\| [0057] Fig. 3 is a process flow diagram showing a method of sequestering carbondioxide using the system of either Fig. IA or IB, in accordance with an embodiment of the present invention;\| [0058] Fig. 4 is a schematic of a heat exchange apparatus, in accordance with an embodiment of the present invention;\| [0059] Fig. 5 is a schematic of a pressure exchange apparatus in accordance with an embodiment of the present invention; and\| [0060] Fig. 6 is a schematic illustrating a metal silicate preparation and grinding technique, in accordance with an embodiment of the present invention.\| [0061] Detailed Description of an Embodiment\| [0062] In the following description, embodiments of the present invention are described in the context of a system, apparatus and method for the capture and sequestration of carbon dioxide contained within flue gases emitted by a fossil fuel-fired power station. However, it is to be understood that the system, apparatus and method could equally be utilised for the permanent sequestration of carbon dioxide from any 'point' source and is not limited to the particular arrangement described herein. With reference to Fig. 1 there is shown a flow diagram of a system 10 for performing a carbon dioxide (CO2) sequestration process from a gas feed stream containing carbon dioxide outputted from a power station, in accordance with a first embodiment of the present invention. With additional reference to Fig. 3, the system 10 is arranged to perform the process 100 of (i) scrubbing a gas stream containing carbon dioxide with a normal ammonium carbonate solution that is able to absorb the carbon dioxide, whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising, in the main, ammonium bicarbonate; and (ii) passing a slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| [0063] In an embodiment the method may further comprise a stage (iii) of contacting flue gases with a circulating dilute normal ammonium carbonate solution that may be chilled to the extent necessary, in a vessel in a counter-current, staged manner so thatresidual ammonia in the flue gases is scrubbed from these gases to levels low enough to allow their final discharge in the atmosphere.\| [0064] In the illustrated embodiment the stages (i) and (iii) are performed within a first apparatus 20 having separate chambers, in the form of an absorption chamber 28 and a scrubbing chamber 30, respectively. Stage (ii) occurs within a reactor either in the form of a pipeline 52 (as shown in Fig. 1) or, as will be described in more detail in subsequent paragraphs with reference to Fig. 2, an underground chamber excavated at a sufficient depth to facilitate conditions for the carbonation reactions to take place. According to Fig. 1, the pipeline 52 may connect the reactor to a mineral quarry site from with metal silicate is sourced.\| [0065] The carbon dioxide sequestration process utilised in embodiments of the present invention is based on mineral carbonation. Mineral carbonation is a reaction between a metal-oxide-bearing mineral material and carbon dioxide. The metal-oxide bearing material may, for example, be alkaline-earth metals. Advantageously, the process 100 does not require the source of carbon dioxide to be particularly pure. In mineral carbonation, carbon dioxide reacts with the metal oxide bearing material to generate insoluble carbonates, that is to say:\| [0066] MO + CO2 → MCO3 + heat (1)\| [0067] which is an exothermic reaction, occurring more rapidly at elevated temperature, typically above 1500C. Certain chemicals may serve to increase the rate at which this reaction proceeds without being consumed themselves, i.e. they serve as catalysts. The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage). Further, embodiments are inherently operable to make bicarbonate ions as carbon dioxide is absorbed into the ammonia-rich ammonium carbonate solution, without having to handle highly pressurized carbon dioxide.\| [0068] The exact nature of the insoluble carbonates formed by the reaction depends on the metal-oxide bearing material. Suitable materials may be naturally occurring alkaline-earth metal-rich silicate rocks which contain mineral constituents such asserpentine (Mg3Si2O5(OH)4), olivine (Mg2SiO4), orthopyroxene (MgSiO3), talc (Mg3Si4O10(OH)2) and wollastonite (CaSiO3). In practice, the element Iron (Fe) may substitute for some of the Magnesium (Mg) or Calcium (Ca). Other suitable materials include alkaline industry residues such as slag from steel production, the ash (both fly and bottom) from pulverised coal-fired boilers, the ash remaining from the combustion of paper recycling residues (de-inking ash), and cement. The amount of heat generated in the reaction will depend on the specific metal and on the mineral containing the metal oxide as can be seen below in the case of three natural silicates (heat values are given per unit mole of CO2 and at standard conditions (25°C and 0.1 MPa):\| [0069] Olivine\| [0070] Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 + 89 kJ moll CO2 (2a)\| [0071] Serpentine Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol" 1 CO2 (2b)\| [0072] Wollastonite\| [0073] CaSiO3 + CO2 → CaCO3 + SiO2 + 90 kJ mol l CO2 (2c)\| [0074] In the illustrated embodiments, the silicate rock comprises the mineral serpentine, Mg3Si2O5(OH)4. AU of the above minerals may be pre-treated to increase the surface area of rock that can subsequently come into direct contact with the carbon dioxide. In an embodiment, the pre-treatment involves crushing, grinding and/or milling of the mineral, as well as some mechanical classification and separation. For example, the minerals could be milled (e.g. wet-milled) in ball mills or equivalent to form a finely ground metal silicate slurry (hereafter 'silicate slurry') 36 wherein 90% of the mineral matter is finer than 40 microns. However, it will be understood that the extent of the pre-treatment is dependent upon the source and type of mineral(s) being used in the process. An example milling and transportation process flow is shown in Fig. 6.\| [0075] Again with specific reference to Fig. 1, the carbon dioxide sequestration system 10 will now be described in detail. The system 10 receives a raw flue gas mixture feed stream 32 that has been generated and subsequently emitted by a powerstation or other point source (not shown). In the embodiment described herein, the raw flue gas mixture 32 is passed though a filter 33 to remove most of the particulate matter. Suitable filters may include fabric filters, electrostatic precipitators and the like. Cleaning the raw flue gas mixture 32 may serve to minimise both the maintenance costs in downstream gas-handling equipment and the concentrations of particulates in flue gases ultimately discharged to the atmosphere. It will be understood, however, that while desirable for process reasons, it is not essential that the raw flue gas mixture 32 be cleaned of all particulates before it enters the scrubbing chamber 30. In an embodiment, the filtering process may additionally involve controlling the level of SOx and NOx that is present within the flue gas so as to adjust the pH level of the ammoniated slurry by virtue of the concentration of sulfate and nitrate ions present in it (which in turn affects the reaction rate between the silicate rocks and carbon dioxide by driving magnesium and calcium ions into solution) as will be described in detail below.\| [0076] To maximise heat recovery in the system 10, the filtered flue gas mixture is then passed through a heat exchange apparatus in the form of a heat exchanger 34 so that the sensible heat of the filtered flue gas mixture (typically at a temperature of around 135°C) is exchanged with the cooler gasses being expelled from the scrubbing chamber 30 of the first apparatus 20 and the filtered flue gas mixture is cooled to its water-vapour saturation temperature (i.e. to about 50°C). Suitable heat exchangers may include, for example, recuperative-type heat exchangers, such as the Ljungstrom rotary design as commonly used for air pre-heating in power stations.\| [0077] As mentioned in preceding paragraphs, the carbon dioxide sequestration system 10 receives a source of silicate slurry 36. According to the embodiment described herein, the silicate slurry source is located near or at the mine site from which the silicate rocks are sourced. As previously described, the silicate mineral sourced from the mine site is finely ground (e.g. by wet-milling in ball mills or equivalent to form the slurry) wherein roughly 90% of the mineral matter is finer than 40 microns or as determined to be appropriate for the proper operation of the process.\| [0078] According to Fig. 1, the silicate slurry 36 is first blended with a solution in water of normal ammonium carbonate to create an ammonia rich ammonium carbonate- metal silicate slurry (hereafter "absorbent slurry"). In the illustrated embodiment, the normal ammonium carbonate salts in solution (hereafter "circulating solution") is the solution in water of most of the normal ammonium carbonate salts accompanying thefinal metal carbonate/silica product. Specifically, according to the Fig. 1 embodiment, the circulating solution represents the overflow of a first thickener 90a of a counter- current decantation (CCD) thickener separation system 90.\| [0079] In flowing from the CCD thickener system 90 to the power station site, the absorbent slurry 47 passes through a first pressure-exchange apparatus 38. To minimise power consumption, the pressure of the absorbent slurry 47 may be increased by exchanging pressure with the final metal carbonate/silica product (hereafter 'final product'), typically to a pressure of approximately 100 Bar. hi addition, to minimise heat losses from the system 10 (and to ensure that the final product is cooled to a suitable temperature before it is emplaced in its final permanent repository), the absorbent slurry 47 passes counter-currently through a heat exchanger 40 to absorb the surplus sensible heat contained in the final product.\| [0080] According to Fig. 1, a pipeline 44 connects the first apparatus 20 to the silicate mineral quarry site and is used to transport the absorbent slurry 47 used in the sequestration process 100. As will be described in more detail in subsequent paragraphs, an alternate path 52 in the pipeline 44, in this embodiment, also serves to act as a controlled reactor in which the metal carbonation reaction largely takes place. At or near to the power station site, the absorbent slurry 47 is passed counter-currently through a second heat exchanger 46 and a second pressure-exchange apparatus 48, where the absorbent slurry 47 is cooled and reduced in pressure by exchange with the reactive slurry discharged from the first apparatus 20, before being fed directly into the scrubbing chamber 30.\| [0081] After arriving at the power station site, a residual circulating stream passes into a vessel in the form of a residual ammonia scrubber 56, in such a way that flue gases that have been stripped of most of their carbon dioxide content, pass upwards from below. There may be any number of counter-current contacting stages, depending only on the desired implementation. The residual ammonia scrubber 56 is operable such that the cleaned, largely carbon dioxide-free flue gases may leave the system with less than one part per million of ammonia, hi order to achieve such low losses of ammonia, the fluid circulating through this vessel may be cooled, even chilled, to an appropriate degree. Specifically, the fluid circulating through this vessel is comprised of the dilute aqueous phase described above (i.e. a clarified, dilute solution in water of normal ammonium carbonate), which enters the vessel and collects in the base of the residualammonia scrubber 56 from where it is circulated by pumps to the header sprays to above the uppermost of the contacting stages. It is this circulating flow that is cooled to the requisite extent, by firstly, arranging for it to flow firstly, through one or more first stage heat exchangers that are cooled by circulating water cooled in turn, in a cooling tower, and secondly, through one or more second-stage heat exchangers that are cooled in turn, by a stream of water or other suitable heat-exchange fluid that has been chilled to below ambient temperatures by a chilling plant suitable for the purpose. In an embodiment, the chilling plant is an ammonia absorption chiller 82, the operating principles of which are understood by those skilled in the appropriate art. It is to be understood however, that alternative types of chilling plant provided they have adequate chilling capacity, are equally suitable.\| [0082] Absorption chillers, including ammonia absorption chillers, require a source of heat for their operation. In an embodiment, some of this heat may be provided by the heat released through carbonation reactions as shown as equations 2a, 2b and 2c, depending on the type of silicate mineral used.\| [0083] The cooled filtered flue gas mixture passing through the heat exchanger 34 enters the scrubbing chamber 30 where the gas mixture passes upwards through deluging sprays of circulating solution entering from the residual ammonia scrubber 56 from above. When carbon dioxide is absorbed in the circulating solution, a further substantial quantity of heat is liberated, as gaseous carbon dioxide is absorbed into it, and reacts with the normal ammonium carbonate salts in the circulating solution. The reactions include the conversion of the normal ammonium carbonate (NELt)2CO3 to the bicarbonate NH4HCO3, via the reaction:\| [0084] (NFLt)2CO3 + CO2 + H2O -» 2NH4HCO3 (3)\| [0085] Normal ammonium Ammonium\| [0086] Carbonate bicarbonate\| [0087] While this will be the main reaction encountered, other reactions may equally occur in parallel including, when there is free molecular ammonia present in the scrubbing solution:\| [0088] NH3 + CO2 + H2O -> NH4HCO3 (3a)As well, some of the ammonium bicarbonate may lose some combined water to form the carbamate, NH2COONH4, hence this compound will likely be present in smaller quantities, perhaps along with some urea, CO(NH2)2, formed when the carbamate loses additional combined water.\| [0089] FURTHER DETAIL OF SEQUESTRATION PROCESS\| [0090] In more detail, the carbon capture process begins with the metal silicate (in this case, ground serpentine) being blended into a circulating solution of serpentine and an aqueous phase containing normal ammonium carbonate in solution to thereby produce the absorbent slurry. The absorbent slurry is then circulated using pumps, through a carbon dioxide absorption chamber 28 which in an embodiment may be the lower half of a tall scrubbing chamber 30 (the upper part being utilised as the residual ammonia scrubber 56). The absorption chamber 28 may, for example, take the form of a flue gas desulfurization scrubber, with the absorbent slurry circulated at high flow rates through banks of sprays.\| [0091] The absorbent slurry is heated by the transfer of latent heat from the flue gases rising from below. Also, as mentioned above, when carbon dioxide gas is absorbed into the absorbent slurry, substantial quantities of heat are liberated, as carbon dioxide reacts with the mainly normal ammonium carbonate (NHi)2CO3, to form the bicarbonate NH4HCO3, as per Equation 3 (there may also be some intermediate salts e.g. the sesquicarbonate (NFLO2CO3. NH4HCO3, the carbamate NH4COONH2, and traces of urea, CO(NH2)2). The heat of solution, along with the latent heat released when water vapour in the flue gases condenses, is removed by circulating the absorbent slurry through water-cooled heat exchangers 84.\| [0092] As mentioned above, the output from the absorption chamber 28 is a reactive solution in the form of a metal silicate slurry in an aqueous phase that is itself a solution of carbonate-rich ammonium carbonates, primarily ammonium bicarbonate. A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor.On route to the mine site, at or near to the power station, the reactive slurry is pressurised at the second pressure-exchange apparatus 48 to a high pressure of around 120 Bar (above the critical pressures of both carbon dioxide and ammonia) and also heated to at least 100°C and preferably to at least 150°C. Heating is accomplished by transferring heat from the incoming silicate slurry arriving from the mine at the heat exchanger 46, and also, if necessary, by injection of steam 54. The heat contained in the incoming silicate slurry in part originates from reactions 2(a), 2(b), and 2(c), depending on the silicate mineral involved. hi the return pipeline 52 of the pipe reactor, at temperatures below 50°C or thereabouts, most if not all of the carbon dioxide present is in the form of ammonium carbonates. When the slurry is heated to at least 100°C under pressures of at least 100 Bar, the tendency is for the various forms of ammonium carbonates in solution to decompose to molecular carbon dioxide CO2 and ammonia NH3. These remain substantially in solution in the reactive slurry under these temperature and pressure conditions. A result of this process is the partial pressure of the carbon dioxide will be particularly high, thereby serving to enhance the speed of reaction with the silicate minerals, converting them to insoluble carbonates and silica during the transit. In an embodiment, the pipeline may be 10 kilometres in length to allow adequate time for the reactions to proceed essentially to completion resulting in the metal carbonate product that contained most if not all of the carbon dioxide originally scrubbed from the power station flue gases. It will be understood that the length may vary, however, depending on the actual implementation.\| [0093] It will be apparent that a high concentration of ammonia is maintained in the slurry throughout its passage from the power station to the silicate rock mine/quarry or other emplacement site.\| [0094] When the final product in the return pipeline 52 reaches the vicinity of the mine site, as described above, the hot pressurised final product transfers its sensible heat via the heat exchanger 40 to the absorbent slurry being pumped towards the power station, hi the process the final product is cooled to a temperature below 50°C. To achieve this temperature in practice, it may be necessary to employ additional cooling to ensure that the temperature of the final product stream is cool enough for the recombination reactions to occur. In an embodiment, the additional cooling is accomplished by means of a heat exchanger cooled by circulating cooling water fromdry (e.g. radiator-type) cooling towers, fin fan coolers, or a natural-draft cooling tower (not shown) such as used for cooling in the power station. A consequence is that free molecular ammonia and carbon dioxide will subsequently re-combine to form ammonium carbonate salts dissolved in the aqueous phase that can be recovered and used in the circulating solution. Since carbon dioxide has been removed from the aqueous phase by reaction with the mineral silicate, the ratio of carbon dioxide to ammonia is lower than it was before the key carbonation reactions occurred. Hence, the predominant form of ammonium carbonate salt formed is normal ammonium carbonate (NKU)2CO3 which, it will be noted, may contain twice as many ammonia units pre carbon dioxide unit as the bicarbonate, NH4HCO3. This is the reason why a solution rich in normal ammonium carbonate may also be referred to as an ammonia-rich ammonium carbonate solution. In any case, it will be understood that other ammonium salts, plus molecular ammonia NH3 and ammonium hydroxide NH4OH, may also be present.\| [0095] FURTHER DETAIL OF SEPARATION SYSTEM\| [0096] As previously mentioned, the final reacted slurry (i.e. containing mainly normal ammonium carbonate in solution together with the carbonate/silica solids that are the products of carbonation) is passed through a solids-liquids separation process. The separation process generally involves producing a clear overflow solution containing most of the ammonium salts and other soluble chemicals (including any molecular ammonia and ammonium hydroxide NH4OH that are dissolved in it) and a dense slurry or even paste-consistency underflow containing all of the solids.\| [0097] Separation may be accomplished by one or more of several means known to those skilled in the art. In an embodiment, a filtration process may be employed using, for example, rotary vacuum filters. In an alternative embodiment, the filtration process may use plate and frame-type filter presses. In both embodiments, a filter cake is formed on a filtration medium (a filter cloth for example) and wash-water is sprayed onto, or otherwise caused to pass through, the filter cake to wash out residual quantities of soluble materials including ammonium carbonate salts. The filter cake represents the first, solids-rich stream, which may be handled as a cake, or converted to a dense slurry by addition of small quantities of additional water sufficient to allow it to be handled asa slurry. The aqueous phase, including wash-water passing through the filter cake and filtration medium, represents the second stream. In another embodiment, separation of the solids from the aqueous phase (specifically, the separation of the ammonium carbonate salts and other soluble materials in the aqueous phase) is achieved by a process known as counter-current decantation (CCD), as illustrated in the Fig. 1 and 2 embodiments. This technique involves utilising a number of continuous thickener tanks (in the illustrated embodiment three tanks are used, although it will be understood by persons skilled in the art that more or less thickener tanks may be employed depending on the desired implementation) that are arranged in a series. The CCD thickener system 90 may recover a substantial amount (e.g. around 99 per cent) of all of the dissolved salts and other soluble substances (including ammonia) in the aqueous phase accompanying the final product. The remaining amount of salts will accompany the final product solids as they are pumped to their final permanent repository.\| [0098] It is noted that in some implementations, only a certain percentage (e.g. 80%) of soluble substances may be recovered by the first thickener 90a of the CCD system 90, with the remainder recovered by subsequent stages. In an embodiment, as shown in Figure 1, the two aqueous-phase streams resulting from the overflows of the first-stage and second-stage thickeners are blended either by arranging for the overflow of the second stage thickener to be blended with the feed stream to the first-stage thickener, or by directly blending the two overflow streams.\| [0099] In more detail, the final products stream from the reactor, after pressure reduction in the pressure exchangers 38 and cooling in the heat exchangers 40, enters the first thickener 90a of the series. The insoluble solids (the carbonated mineral) suspended in the feed stream settle in the thickener tank 90a to form a dense slurry that is withdrawn as an underflow stream. The balance of the feed entering the thickener tank overflows as a clarified supernatant, which contains most of the soluble ammonium carbonate salts and other soluble materials (i.e. the circulating solution). The underflow may still contain around 10 per cent of the aqueous phase that first entered the thickener, and it is the function of the balance of thickeners in the CCD system to recover these salts to the maximum practicable extent, from the insoluble solids that are to be finally emplaced. In the CCD system 90, the underflow slurry from thickener tank 90a is pumped to the next thickener tank 90b in line. Also fed to tank 90b is the clarified overflow from thickener tank 90c, and so on. Where "N" thickenertanks are employed, the final thickener tank in the series, tank N, receives a feed stream which is a mixture of the underflow of thickener tank N-I, and fresh water, which may be replaced in part by any surplus aqueous phase recovered from final emplacements of carbonated mineral as this further consolidates and/or drains from the mineral, over time. In an embodiment, a mixture of thickener tanks, one or more stages in series, and filtration units may be used to effect the separation of soluble ammonium carbonate salts from the insoluble carbonated mineral.\| [0100] The dense slurry stream (in one embodiment a filter cake, in another embodiment the underflow of CCD thickener Unit N) is the final product slurry substantially free of salts, and in a form suitable for permanent emplacement in mine voids or other purpose-built repositories (not shown). In these emplacements the solids can settle and consolidate, releasing additional aqueous phase as a clear supernatant. This supernatant may also be collected and re-used in the process, as described in the paragraph above. When the CCD system 90 for the recovery of ammonium salts is close to the power station, as may be the case for the underground chamber reactor embodiment (Fig. 2), it may be appropriate to add the remainder of the power station fly ash to the final product slurry from the carbon sequestration process, so the two streams may be handled and co-disposed of as a single stream. An advantage stemming from the presence of fly ash having pozzolanic properties (a tendency to "set" in the presence of alkalis and moisture) in the final product, is that it will assist with the rehabilitation process, by encouraging the final product/fly ash mix to "set", thereby immobilising the contents of the emplacement. hi an embodiment the overflow of the second stage of the CCD thickener system 90, being a relatively dilute, clarified (insoluble solids- free) solution in water of ammonia-rich ammonium carbonate salts may be handled separately (see Fig. 2). hi such an embodiment, the stream (hereafter "residual stream") is sent overland from the CCD system 90 (installed near the silicate quarry) to the power station site via a separate, third pipeline 91. Pumps raise the pressure of the contents of the third pipeline 91 to the extent necessary for them to traverse the length of the pipeline 91. However, it will be understood that the third pipeline 91 may be configured to accept some of the heat and some of the pressure energy released when the pressure and temperature of the final products pipeline are reduced via heat- and pressure-exchange equipment.Whether the third pipeline 91 is configured in this way, or simply used as a conduit for the return of this stream to the power station site, depends on the individual circumstances of the installation.\| [0101] 5 CHEMICAL REACTIONS\| [0102] The main chemical processes occurring throughout the process are as follows: 3CO2 + 3(NH4)2CO3 + 3H2O -» 6NH4HCO3 (4)\| [0103] 6NH4HCO3 -> 6NH3 + 6H2O + 6CO2 (5)\| [0104] 6CO2 + Mg3Si2O5(OH)4 -» 2SiO2Φ + 3MgCO3Ψ + 2H2O 0 + 6NH3 + 3CO2 (6)\| [0105] 3CO2 + 6NH3 + 3H2O -» 3(NILO2CO3 (7)\| [0106] NH3 + NH4HCO3 -» (NILO2CO3 (8)\| [0107] Equation 4 represents the absorption of carbon dioxide into the ammonia-rich5 ammonium carbonate aqueous phase to produce a solution comprising ammonium bicarbonate. On heating under pressures of at least 100 Bar in the reactor (i.e. pipeline or underground chamber), this ammonium bicarbonate decomposes to molecular ammonia, water and carbon dioxide according to equation 5. As shown in equation 6, under the high pressure and temperature conditions prevailing in the reactor the carbon O dioxide reacts with the serpentine (the chemical formula of which is shown in equation 6) or other silicate rock to form insoluble metal carbonates and silica, the final products of the process, which store the carbon dioxide. Equation 7 describes what happens after the reaction products are cooled to below 50°C, i.e. low enough to allow the free molecular ammonia and carbon dioxide to combine to form ammonium carbonate salts5 in solution. As shown, since much of the carbon dioxide has been absorbed by the metal silicate (here serpentine) the ratio of ammonia to carbon dioxide favour formation of the ammonia-rich normal carbonate. Additional normal ammonium carbonate may form according to equation 8, by reaction between ammonium bicarbonate, and free molecular ammonia. 0CONTROLLING ACIDITY IN THE SYSTEM\| [0108] As mentioned in preceding paragraphs, sulfate ions from SOx, and nitrate ions from NOx respectively, contained in the raw flue gases, may accumulate in the circulating solution of ammonium salts. Oxides of sulfur (SOx) are inevitable byproducts of the combustion of fossil fuels including coal, that incorporate sulfur- containing compounds in reduced form, for example pyrite (iron disulfide FeS2). Oxides of nitrogen (NOx) are also inevitable byproducts of the combustion of fossil fuels including coal, originating from nitrogen-containing compounds in the fuel, and from reactions between oxygen and nitrogen in air induced by the heat of the fuels' combustion, hi an Australian context, where coals tend to have low sulfur contents, and assuming use of modern "low-NOx burners", the rates of build-up of nitrate ions will not be high, but their build-up may still need to be limited to maintain the pH range to that most suited for the overall processes. When the SOx and NOx contained in flue gases contact the absorbent slurry as encountered in the scrubbing chamber 30 in the presence of additional oxygen including that contained in flue gases, a series of reactions occur that convert these gases to sulfates and nitrates: SOx to sulfate ions SO4— , and NOx to nitrate ions NO3-. In the normal course of separating out the insoluble solids for example magnesite and silica formed from the reactions between carbon dioxide and the metal silicates, as previously described, the soluble salts dissolved in the aqueous phase from the reactor including sulfates and nitrates are recycled for re-use in the scrubber, apart from the small quantities of such salts that are ultimately emplaced with the final product metal carbonates and silica. A consequence is that while carbon dioxide entering the system forms additional carbonate ions that are ultimately removed at an equal rate as insoluble metal carbonates, the tendency is for both sulfate and nitrate ions to accumulate in the circulating aqueous phase. In an embodiment, the system may implement a process for limiting the build-up of these ions (anions) to avoid an increase in the acidity (reduction in the pH number) of the circulating solution, as the formation of these ions leads to a concomitant formation of hydrogen ions in solution. It is noted that the system, to some extent, may inherently limit such a build-up by virtue of the fact that, as mentioned in the previous paragraph, not all soluble salts and other dissolved substances will be recovered by way of the solids-liquids separationprocess. To further reduce nitrate ion equilibrium concentration, it is necessary to limit correspondingly, the concentrations of NOx gases in the flue gases entering the scrubbing vessel 30. This may be achieved, for example, by using so-called 'low-NOx burners', and by other methods which achieve control of the combustion process to limit NOx formation in the power station's boilers.\| [0109] To control concentrations of sulfate ions in the circulating aqueous phase, the system 10 may employ an additional control mechanism 96 arranged to add/feed appropriate quantities of calcium oxide or hydroxide (which in water form calcium ions and hydroxyl ions) to a portion of the circulating slurry (a side-stream), wherein the sulfate ions react with it to form calcium sulfate, which mostly precipitates out as the sparingly soluble hydrated salt, gypsum:\| [0110] SO4" + Ca+* + 2H2O -» CaSO4.2H2O Ψ (9)\| [0111] Meanwhile, the hydroxyl ions combine with and neutralise a corresponding number of hydrogen ions (to form water molecules), thereby controlling (reducing) the acidity of the circulating solution.\| [0112] In an embodiment, calcium oxide generally may be naturally present in the power station fly ashes. If present in sufficient concentrations, the appropriate quantities of fly ash may be added by the control mechanism 96 to the circulating solution to control the pH levels to the desired ranges. If the quantities of calcium oxide naturally present in fly ash are inadequate, they may, in an embodiment, be augmented by adding pulverised limestone to raw power station flue gases in the boilers at one or more locations for example immediately upstream of the economiser section of the boilers, where flue gas temperatures are appropriate for the decomposition of limestone to calcium oxide and carbon dioxide (when exposed to furnace temperatures of 1,0000C or more, limestone is calcined to quicklime.\| [0113] Treatment processes applied to this side stream may also incorporate steps to recover base metals and other valuable components in solution, including nickel, copper and iron, hi one form, side-stream treatment may involve adding an inexpensive alkali, e.g. calcined lime, dolomite, limestone or the like. Sulfate ions can be removed via the following equation (shown for normal ammonium sulphate and calcium oxide):(NILt)2SO4 + CaO + 3H2O -» CaSO4.2H2θΨ + 2NH4OH (10) ammonium quicklime gypsum ammonium\| [0114] Sulfate hydroxide\| [0115] In an embodiment the control mechanism 96 may be further arranged to add fresh ammonia to the circulating solution, at an appropriate rate, to account for any losses of ammonia.\| [0116] FURTHER DETAIL OF ABSORPTION/SCRUBBING CHAMBER OPERATION Conditions in the absorption chamber 28 may be strongly oxidising to assist the conversion of the impurity gases dissolving in the aqueous phase of the slurry (i.e. SOx ending up as sulfates rather than sulfites, and NOx ending up as nitrates rather than nitrites). In an embodiment, the cool, saturated condition of the flue gases when in the absorption chamber 28, plus the partial pressure of oxygen in these gases of three per cent or more, may be sufficient to ensure oxidising conditions. As well, the large pool of slurry held in the bottom of the absorption chamber 28 may be aerated using compressed air as is normal practice with flue gas desulfurisation (FGD). However, if additional oxidising is required, the process may further involve irradiation of the flue gases immediately upstream of their entry into the absorption chamber 28 by electron beams or high- voltage brush discharge, to form free radicals from water and oxygen (OH" and 0~). These are powerful oxidising agents, able to convert rapidly, sulfur dioxide SO2 to the trioxide SO3, and nitric oxide NO to the dioxide NO2, the precursors to sulfates and nitrates respectively. Thus, the absorption chamber 28 may serve as a highly efficient scrubber for the removal of SOx and NOx. It may also remove volatile metals that may exist in trace quantities in coal and that end up in flue gases notably mercury (the low operating temperatures and oxidising environment will tend to favour the conversion of any mercury vapour present to non- volatile mercuric oxide, an insoluble solid that will accompany the final product metal carbonate and silica to their permanent emplacement).\| [0117] FURTHER DETAIL OF PRESSURE EXCHANGERS\| [0118] With reference to Fig. 4, there is shown an arrangement for the pressure- exchange apparatus described above. At the end of the reaction process, the pressure ofthe final carbonate-rich product must be reduced from approximately 120 Bar to atmospheric pressure. Instead of merely reducing pressure by throttling valves, thereby losing the energy embodied in this pressure, the energy this pressure represents may be conserved by transferring it to the extent possible, to the silicate slurry. In Fig. 4, slurry A comprises the products of the reactions that occur as the ammoniated, carbonated silicate slurry flow through the pipeline 44 from the power station to the mine site; while slurry B represents silicate slurry from the mine. A consequence of pressure exchange in these two stages is that slurry A's pressure would fall from around 120 Bar to near ambient pressure, while that of slurry B would rise from around atmospheric pressure to perhaps 100 Bar.\| [0119] Another pressure-exchange apparatus is also utilised at the power station site. Here, using the terminology of Fig. 4, slurry A represents the hot silicate slurry arriving via the pipeline from the mine; while slurry B comprises slurry exiting the scrubbing chamber 30 (i.e. silicate slurry now charged with ammonia and carbon dioxide, but at close to ambient pressures). A consequence of pressure exchange in this stage is that slurry A's pressure would fall from its arrival pressure (this may be 120 Bar, a pressure that would be maintained by booster pumping stations at strategic locations along the pipeline 44 to overcome friction losses), to near ambient pressure. This pressure may be transferred (exchanged) to the extent possible to slurry B, thereby minimising the amount of pumping energy required to raise the pressure of this slurry to the levels required, here assumed to be 120 Bar. Since slurry A at this point will be at well below 120 Bar, pressure-exchange between slurries A and B alone may not be capable of raising the pressure of slurry B to 120 Bar. Also, the volume of slurry B may exceed that of slurry A. This is because of the much higher contents of carbon dioxide and ammonia, and of water condensed out of the power station flue gases. In an embodiment, additional pumping capacity may be installed to boost slurry B pressures to those required for the pipeline 44, and to pressurise those (relatively small) quantities of slurry B that cannot be pressurised by pressure-exchange with slurry A. For this function, conventional high-pressure diaphragm pumps, such as the Geho pump manufactured by Weir Netherlands b.v., may be implemented. This pumping, together with the pumping energy required to maintain pressures along the length of the pipelines, account for a substantial proportion of the total mechanical energy input to the total process. Other suitable pressure exchange/pump-turbine sets may comprisecentrifugal pumps and radial-type hydraulic turbines. As the pressures are relatively high, the type of centrifugal pump may be a multi-stage barrel-type pump.\| [0120] With reference to Fig. 5 there is shown a configuration for the heat exchanger arrangements 40 & 46, according to an embodiment of the present invention. As previously discussed, high temperatures are required to initiate and accelerate the carbon sequestration reactions: the conversion of metal silicates to carbonates. These reactions, being exothermic, yield additional heat that can and should be applied to assist with creating the conditions needed for these reactions to proceed most efficiently. As shown, the heat-exchanger arrangement is in the form of a simple shell- and-tube heat exchanger, consisting of two concentric pipes: the inner forms the "tube", the outer, the "shell". An advantage with this arrangement is that the heat exchanger can be made as long as is required to affect the desired transfer of heat: if necessary, many hundreds of metres long. For heat exchanger 40 (i.e. the heat exchanger on the silicate rock quarry site side), heat energy is transferred between the final carbonate/silica product (i.e. slurry A), which is hot, and the silicate slurry (slurry B), which is cool. For heat exchanger 46 (i.e. the heat exchanger on the power station side), slurry A would be hot silicate slurry from the quarry, while slurry B would be slurry exiting the scrubbing chamber 30 (i.e. now charged with ammonia and carbon dioxide, but at close to ambient temperatures).\| [0121] UNDERGROUND REACTOR\| [0122] Turning now to Fig. 2, there is shown an alternative system 200 for performing carbon dioxide sequestration which utilises (where geological conditions permit) an underground chamber as the reactor, as opposed to a pipeline reactor as illustrated in Fig. 1. In this embodiment, the reactor is in the form of a chamber 70 excavated from bedrock at a depth sufficient to allow the conditions for the core carbonation reactions to be generated entirely or partly by static head alone (e.g. 100 Bar). A chamber 70 excavated at a depth of approximately 800 meters and having a volume of 300,000 cubic meters, sufficient to allow for a 24 hours' detention time for the contents, may be envisaged for holding the reactive slurry output from a system 200 fitted to an efficient\| [0123] 1,000MWe coal-fired power station. In practice a smaller chamber may suffice, should it arise that the reactions are essentially completed in less time.\| [0124] The silicate slurry 36 may be prepared either at the serpentine quarry site andpumped overland to the power station site, or, the mineral could be railed, trucked or otherwise suitably transported to the power station site, and prepared there. Were the former implementation adopted, pipeline arrangements 44 would be considerably simpler than for the pipeline reactor embodiment described above with reference to Fig. 1. Specifically, the silicate slurry 36 would not be required to collect and transport heat and pressure energy from the quarry site to the power station site, nor to host any residual ammonium salts. The pipeline 44 would simply be utilised for mineral transport; whether it was transported as a lump product by rail or as slurry by pipeline would be determined by economic and environmental considerations. It will be appreciated that in this embodiment, silicate slurry density may be substantially higher (e.g. 60 per cent solids by weight), thereby reducing the volumes of silicate slurry required to be pumped, and allowing a lower pipeline velocity because of the reduced tendency for the solids in denser slurries to segregate and silt up the pipeline 44. Also, arrangements for conserving heat and pressure are much simpler than they would need to be for the pipeline reactor alternative.\| [0125] In Fig. 2, an injection pump 72 is utilised to drive the circulation of the reactive slurry from the scrubbing chamber 40, through a plurality of counter-current heat exchangers 74, 76, underground reactor 70 and counter-current decantation system for the separation of normal ammonium carbonate and other salts in the aqueous phase of the products of the underground reactor, and the insoluble carbonated mineral solids that are to be emplaced permanently.\| [0126] Heat exchangers 74, 76 are shown in schematic form at two locations on Fig. 2. The heat exchangers 74, 76 may be long, shell-and-tube designs, as shown in Fig. 4: they may span most of the vertical distance from the scrubbing chamber 40 down to the underground chamber 70. This is to say, whereas two separate pipelines are implied in Fig. 2, in practice, for most of their length they may be concentric: the annulus formed between the outer and concentric inner pipe transporting the hot reaction products, while the inner pipe transports the products heading downward to the Reaction chamber. It will be understood by persons skilled in the art that this selection may be reversed.\| [0127] In contrast to the pipeline reactor configuration shown in Fig. 2, heating of the reactive slurry may be accomplished by exchanging heat from the hot reaction productsrising first from the ammonia gas recovery vessel 78, and as the raw slurry descends further, from hot slurry rising from the underground chamber 70. While some supplementary heat may be required, the heat generated by Equation 2(b) would be conserved, and available to heat raw reactive slurry. The design of the underground chamber 70 may be optimised to achieve some plug- flow characteristics. In an embodiment, the chamber 70 may have a high length- to-diameter ratio of 10: 1 and be vertically aligned. Utilising a vertically aligned chamber provides that the incoming reactive slurry, being cooler hence slightly denser than the average contents of the reactive chamber 70, will tend to stratify at lower levels, displacing hotter slurry upwards. In an embodiment, the underground chamber 70 may be subdivided into two or more vertically stacked sub-chambers.\| [0128] In an embodiment, the reactive chamber 70 may employ an agitator (not shown) to maintain the solids in suspension. This may be advantageous where large residence times are required, implying in turn large reactor volumes. As will readily be appreciated, heat losses from the underground chamber 70 and pipelines may be much smaller than they would be even from a lagged above- ground pipeline and may be further reduced by insulation surrounding the reactor, pipelines and any other underground process vessels. Whereas an overland pipeline represents a plug-flow reactor, ideal conditions for a relatively slow series of reactions as are involved in carbon sequestration are also obtained in the embodiment illustrated in Fig. 2.\| [0129] It is noted that in the Fig 2 embodiment, the two overflow streams from the CCD system are handled separately. The overflow of the first thickener tank 90a is blended with the silicate slurry 36, incoming from the quarry site to form the circulating solution to be sent to the absorption chamber 28.\| [0130] The balance of the process in relation to sequestration, separation and emplacement is as for the overland pipeline reactor case.Example\| [0131] Again with specific reference to Fig. 3, a non-limiting example process flow for carbon sequestration for the first system configuration 10 described herein (i.e. the system depicted in Fig. 1) will now be given, wherein for convenience, like parts to those shown in the foregoing embodiment have been numbered with like numerals.\| [0132] Example 1\| [0133] Table 1: Indicative mass balance figures from 1.000 MWe of black coal-fired electricity generation plant. Material Per year Per hour\| [0134] Total CO2 generated: 6.4 m. tonnes 80O t\| [0135] (NKU)2CO3 to absorb 90% of this CO2 1,60O t\| [0136] Resulting quantity OfNH4HCO3 formed 2,400 1\| [0137] Water to make up 25% solution OfNH4HCO3 7,200 t Serpentine to absorb 90% of this CO2, 80% eff. 17.2 m tonnes 2,150 t\| [0138] Total slurry with NH4HCO3: 9,350 t\| [0139] Slurry density: 1.2 t/m3 1.2 t/m3\| [0140] Slurry volume, m3 8,000 m3\| [0141] Product (carbonate plus silica) solids: 20.6 m. tonnes 2,600 1 Slurry pipe dia. with 3 m/s velocity: 1.0 metres 1.0 metres\| [0142] Ammonia lost due to SOx (90% recovery via Eq. 10) ) 11,,66000O 1t 0.2 t\| [0143] Ammonia lost due to NOx 3,0001 0.37 t\| [0144] Total losses of ammonia: 4.600 1 0.57 t\| [0145] Table 1 provides an indicative detailed mass balance for a carbon dioxide sequestration process, assuming:\| [0146] - 90 per cent carbon dioxide capture and sequestration from 1,000 MWe of black coal- fired electricity generation plant, which when operating in base-load mode might expect to generate annually 8,000 GWh of electricity; - where on a dry ash-free basis, the coal is 81.3% by weight carbon and 0.65% sulphur (as S) and the flue gases contain 400 ppm NOx.An advantage of the carbon dioxide sequestration process 100 and systems 10, 20 according to embodiments of the present invention is that by selecting ammonia as a catalyst/promoter, a single integrated process can be provided for both capture and sequestration of carbon dioxide. In an embodiment, sequestration of the carbon dioxide takes place in a reactor, in the form of a return pathway 52 of a pipeline 44, which advantageously connects the power station (i.e. the source of carbon dioxide) to the source/destination of the absorbent material being used in the process, hi an alternative embodiment, where geological conditions permit, the reactor may take the form of an underground chamber which advantageously facilitates the reaction without requiring pressure-exchange and head-recovery equipment required for the pipeline embodiment. Another advantage of the carbon dioxide sequestration process and systems is that the reaction kinetics may be improved by using ammonia. Therefore, by using ammonia and exploiting the heat generated by the exothermic reaction, the energy consumption of the process 100 can be kept to a minimum. As the reaction products are thermodynamically stable, carbon dioxide can be stored in a permanent stable solid form. Following from this, further advantages include lower operating and capital costs.\| [0147] Persons skilled in the art will appreciate that further advantages may arise from carrying out certain steps of the aforementioned embodiments in isolation. For example, the catalytic effect of a solution of ammonia with an ammonium salt (that may be ammonium carbonate formed by exposing an ammonia-rich solution to a gas stream containing carbon dioxide) in the carbon dioxide sequestration process can also be utilised for extracting metals (e.g. magnesium, iron, nickel, copper and other metals present in the silicate rock) from metal silicates, such as magnesium-rich metal silicates. In such an embodiment a solution of ammonia-rich ammonium carbonates in water may be mixed with a metal silicate (typically in slurry form) to allow the dissolution of magnesium ions by ammonia to recover the metal, in this embodiment a metal compound in the form of magnesium carbonate. The mixing may occur in an ammonia absorption chamber such as that previously described in connection with the preceding embodiments. Preferably the solution contains molecular ammonia in the presence of ammonium salts in solution, such as ammonium carbonate, to prevent the precipitation of magnesium hydroxide, hence allowing the dissolution of magnesium ions by ammonia to continue, substantially free of concerns over tendencies for otherwiseinsoluble magnesium hydroxide to coat, and restrict access to the silicate mineral by carbon dioxide and ammonia. A further advantage arising from this process is that after extraction of magnesium carbonate, other minerals (metals) present within the silicate rock are also amenable to recovery. The silicate rock may comprise mafic or ultra- mafic rocks (i.e. rocks with respectively a high or very high ratio of magnesium to silicon content).\| [0148] Expressed another way, the catalytic effect of the ammonia follows from its tendency to form complexes (ammines) with certain metal ions including magnesium (Mg2+), divalent iron (Fe2+), copper (Cu2+) and nickel (Ni2+). The presence of ammonium salts notably the various carbonates formed from the reaction between ammonia and carbon dioxide prevents precipitation of the otherwise insoluble magnesium hydroxide. Magnesium carbonate is however insoluble in such an environment, so a precipitate of this compound will form from the reaction between magnesium hydroxide and ammonium carbonate, to yield ammonium hydroxide and free molecular ammonia in solution, the latter continuing to extract additional magnesium and other metals from the silicate rock through formation of ammine complexes until all such susceptible metals have been extracted.\| [0149] Finally, it is to be appreciated that various alterations or additions may be made to the parts previously described without departing from the spirit or ambit of the present invention. The process is not limited to having a single two-stage continuous reactor, or a single tube-like reactor, as the process may be arranged to utilise alternatively configured items of equipment as necessary to accommodate process variables, arising from different source materials, capital and operating costs. For example, in the exemplary embodiment previously described the plant design is based on the emission of 800 tonnes CO2/GWh generated from a state-of-the-art black coal- fired electricity generation plant. By comparison, the Bayswater Power Station and the Liddell Power Station, both in the Hunter Valley of New South Wales, Australia, able to generate 2,640 MWe and 2,040 MWe respectively, being older hence less efficient can be expected to emit between 850 and 900 tonnes CO2/GWh. Thus the concentration and rate of carbon dioxide emissions in the flue gas emitted by the power plant may vary such that the plant equipment design may be reconfigured to accommodate these variables. For example, alternative equipment can be configured for the various heat and pressure exchange stations. The carbon dioxideabsorption zone and the scrubbing zone may be arranged in series in two separate vessels (rather than the nested configuration shown in Fig. 1). The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s). As well, the corresponding solids concentration in the slurry feed may be higher or lower than 25% solids by weight. It is possible that the metal silicate solution may comprise a blend of metal silicates, e.g. mixture of serpentines and olivines, even pyroxenes. The reaction kinetics may require heat to be removed from the reactive solution (rather than heat addition as described above). These factors will impact and alter the system pressures. There might be two or more pipelines for transporting the metal silicate solution and the reactive solution; because there are more pipelines, additional heat exchangers and pressure-exchange apparatus may be used. The power station flue gas may include additional pre-processing steps including flue gas desulphurisation (FGD) and selective catalytic reduction (SCR) to reduce concentrations of SOx and NOx respectively hence losses of ammonia from the system. Furthermore, the availability of services, such as steam and cooling water may require different equipment arrangements.\| [0150] Any reference to prior art contained herein is not to be taken as an admission that the information is common general knowledge, unless otherwise indicated.\| [0151] In the claims which follow and in the preceding description of the invention, except where the context requires otherwise due to express language or necessary implication, the word "comprise" or variations such as "comprises" or "comprising" is used in an inclusive sense, i.e. to specify the presence of the stated features but not to preclude the presence or addition of further features in various embodiments of the invention.	(WO2010/088738)\|[0001] SYSTEM, APPARATUS AND METHOD FOR CARBON DIOXIDE\| [0002] SEQUESTRATION\| [0003] Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\| [0004] Background to the Invention\| [0005] There is increased focus on reducing carbon dioxide emissions to the atmosphere, to help minimise the effects of global warming. Carbon dioxide sinks exist naturally, with the main naturally occurring sink being the ocean. Plants are also an effective form of carbon dioxide sink and use photosynthesis to remove carbon from the atmosphere by incorporating it into biomass. However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\| [0006] A major source of harmful carbon dioxide gases are large fossil fuel power stations which, when fuelled by black coal, on average typically output around 0.8 to one tonne of the gas for each MegaWatt-hour (MWh) of electricity they generate. For example, a large power station such as the 2,640 MW Bayswater in the Hunter Valley of New South Wales, Australia, in generating 20 million MWh of electricity in a year, would also output 18 million tonnes of carbon dioxide. It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations. It would also be advantageous if a system and method were provided for the disposition of the gas to be independently audited in perpetuity.\| [0007] Summary of the Invention hi a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| [0008] (i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium carbonate that is able to absorb the carbon dioxide, whereby thecarbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate;\| [0009] (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| [0010] In the context of the present specification, the phrase "solution rich in normal ammonium carbonate " will be understood as referring to a solution whereby the main salt present corresponds to the formula for the normal form of ammonium carbonate\| [0011] (NILO2CO3.. There solution may, however, consist of other ammonium carbonate salts, and there may also be some molecular ammonia NH3, and ammonium hydroxide NH4OH, also present. Further, it should be noted that the terminology "gas stream containing carbon dioxide" does not mean that the stream contains only carbon dioxide, and may contain other off gases.\| [0012] hi an embodiment the metal silicate rock is mixed with the normal ammonium carbonate solution prior to absorbing the carbon dioxide in step (i).\| [0013] hi an embodiment the reaction causes the bicarbonate in the presence of the metal silicate to partially decompose so as to produce an aqueous phase enriched in molecular ammonia and carbon dioxide.\| [0014] hi an embodiment the method comprises the further step of cooling the aqueous phase such that free ammonia and carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered for re-use in step (i) of the process.\| [0015] hi an embodiment the method comprises the further step of adding an alkali to the recovered ammonium carbonate in solution prior to being re-used in step (i). The alkali may be calcium oxide and/or hydroxide, hi an embodiment the calcium oxide is extracted from gas stream prior to scrubbing in step (i).In an embodiment the method comprises the further step of introducing pulverised limestone into a source producing the carbon-dioxide rich gasses. The source may be a coal-fired power station boiler and the pulverised limestone is added upstream of an economiser section of the power station boiler.\| [0016] In an embodiment a portion of the mixed solution used to scrub the gas stream prior to discharge to the atmosphere is chilled to ensure that a quantity of free ammonia in the gases is below a threshold level. The threshold level may, for example, be set by the relevant government or other regulatory body.\| [0017] In an embodiment the step of scrubbing the gas stream comprises exposing the carbon dioxide-containing gas stream to the slurry as a spray or deluge operable to maximise the area of exposure between the slurry and the carbon dioxide-containing gas.\| [0018] In an embodiment the step of controlling the reactor comprises elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\| [0019] In an embodiment the reactor is a pipeline. The pipeline may comprise multiple flow paths and wherein the reaction takes place along the length of one of the flow paths. Another of the flow paths is utilised to supply the metal silicate slurry to the first stage.\| [0020] In an embodiment the method comprises the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\| [0021] In an embodiment the reactor is a chamber located in use underground. The chamber may be located at a depth that provides sufficient pressure by way of static head to enhance the reaction between the carbon dioxide and the metal silicate.In an embodiment the method comprises the further step of grinding a metal silicate rock to produce the metal silicate slurry. The metal silicate slurry may comprise roughly 25% by weight finely ground metal silicate solids.\| [0022] In an embodiment the metal silicate is a magnesium-rich silicate. In an embodiment the magnesium rich silicate is a serpentine and/or olivine and/or pyroxene mineral all commonly described as ultrabasic or ultramafic minerals.\| [0023] In an embodiment the method comprises the further step of cooling the normal ammonium carbonate-metal silicate slurry prior to it use in scrubbing carbon dioxide from flue gases.\| [0024] In accordance with a second aspect of the present invention there is provided a system for sequestering carbon dioxide from a gas stream, the system comprising: (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and\| [0025] (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\| [0026] In an embodiment the first apparatus comprises an absorption chamber arranged to circulate the normal ammonium carbonate solution through the carbon dioxide to thereby absorb the carbon dioxide.\| [0027] hi an embodiment the reactor is the pipeline as used in the method according to the first aspect.\| [0028] In an embodiment the reactor is the chamber used in the method according to the first aspect.In an embodiment the reaction of the bicarbonate with the metal silicate further produces an aqueous phase containing molecular ammonia, carbon dioxide and water.\| [0029] In an embodiment the system further comprises a cooling arrangement arranged to cool the aqueous phase such that free ammonia and remaining carbon dioxide molecules combine to form ammonium carbonate salts in solution, the ammonium carbonate salts in solution arranged to be recovered by a recovery arrangement for reuse by the first apparatus.\| [0030] In an embodiment the system further comprises a separation system arranged to separate the recovered ammonium carbonate in solution from the insoluble metal carbonate-silica phase prior to recovery. The separation arrangement may, for example, be a counter-current decantation (CCD) system comprising one or more stages for separating the solution.\| [0031] In an embodiment the system further comprises a control arrangement arranged to add an alkali to the recovered ammonium carbonate in solution prior to returning it to the first apparatus for re-use.\| [0032] In an embodiment the alkali is calcium oxide and/or hydroxide. The calcium oxide is extracted along with other suspended solids (fly ash solids) from the gas stream prior to scrubbing.\| [0033] In an embodiment the system further comprises a feeder arranged to feed pulverised limestone into a source producing the carbon-dioxide rich flue gases. The point source may, for example, be a coal-fired power station and the pulverised limestone is fed into raw flue gases upstream of the power station boiler's economiser.\| [0034] In an embodiment the metal silicate comprises a magnesium rich silicate as used in the method according to the first aspect.In an embodiment the system further comprises an ammonium carbonate salt recovery arrangement arranged to recover ammonia and ammonium salts accompanying the final product.\| [0035] In an embodiment, the system comprises a solids-liquids separation system arranged to separate and recover ammonium carbonate salts, from the metal carbonate solid product that is sent for final emplacement.\| [0036] hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and produce a metal carbonate and silica.\| [0037] In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the ammonium bicarbonate and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\| [0038] In an embodiment the slurry provided to the chamber is the reactive slurry produced in the process of the first aspect.\| [0039] In an embodiment the method comprises the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber.\| [0040] In an embodiment the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.In accordance with a fifth aspect there is provided a power station or other point source of carbon dioxide-rich flue gases, such as a blast furnace as used in steel making, or a cement kiln, utilising a carbon sequestration system in accordance with the second aspect, the system arranged to capture and sequester carbon dioxide from flue gas emitted by the power station or other point source.\| [0041] In accordance with a sixth aspect, in an ammonia absorption process in which a metal silicate rock is mixed with a normal ammonium carbonate salt solution in water so as to produce a normal ammonium carbonate salt solution in water/metal silicate slurry (the ammoniated slurry) for use in a carbon dioxide sequestration process, there is provided the step of chilling the ammoniated slurry to limit losses of ammonia in scrubbed flue gases to the extent necessary to meet emission limits applying at the location in question.\| [0042] hi an embodiment, the process comprises the further step of providing the ammoniated slurry to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammoniated slurry to thereby absorb the carbon dioxide into a reactive slurry.\| [0043] In accordance with a seventh aspect of the present invention there is provided a method of extracting a target metal from a metal silicate comprising the step of mixing the metal silicate with an ammonia-rich ammonium carbonate salt solution, and reacting the mixed solution to cause the target metal to dissolve into the solution.\| [0044] In an embodiment the method comprises the further step of grinding the metal silicate and forming it into a slurry prior to mixing the metal silicate with the solution.\| [0045] In an embodiment the metal silicate is a magnesium-rich silicate.\| [0046] hi an embodiment the magnesium-rich silicate is a serpentine and/or olivine and/or pyroxene silicate mineral commonly described as an ultrabasic or ultramafic mineral.In an embodiment the solution comprises normal ammonium carbonate salts dissolved in water (the ammoniated solution).\| [0047] In an embodiment the target metal dissolves into the solution and then precipitates in the presence of carbon dioxide, as a metal carbonate to be removed for recovery.\| [0048] In an embodiment the target metal is one or more of magnesium, calcium or iron. The dominant metal within the metal silicate may comprise magnesium.\| [0049] In an eighth aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| [0050] (i) in a first stage, mixing a slurry of a metal silicate rock with a normal ammonium carbonate solution so as to produce a normal ammonium carbonate salt/water/metal silicate slurry;\| [0051] (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the chilled solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| [0052] (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\| [0053] Brief Description of the Drawings\| [0054] An embodiment of the present invention will now be described, by way of example only, with reference to the accompanying drawings, in which:\| [0055] Fig. 1 is a schematic of a carbon dioxide sequestration system according to an embodiment of the present invention;\| [0056] Fig. 2 is a schematic of a carbon dioxide sequestration system according to an alternative embodiment of the present invention;\| [0057] Fig. 3 is a process flow diagram showing a method of sequestering carbondioxide using the system of either Fig. IA or IB, in accordance with an embodiment of the present invention;\| [0058] Fig. 4 is a schematic of a heat exchange apparatus, in accordance with an embodiment of the present invention;\| [0059] Fig. 5 is a schematic of a pressure exchange apparatus in accordance with an embodiment of the present invention; and\| [0060] Fig. 6 is a schematic illustrating a metal silicate preparation and grinding technique, in accordance with an embodiment of the present invention.\| [0061] Detailed Description of an Embodiment\| [0062] In the following description, embodiments of the present invention are described in the context of a system, apparatus and method for the capture and sequestration of carbon dioxide contained within flue gases emitted by a fossil fuel-fired power station. However, it is to be understood that the system, apparatus and method could equally be utilised for the permanent sequestration of carbon dioxide from any 'point' source and is not limited to the particular arrangement described herein. With reference to Fig. 1 there is shown a flow diagram of a system 10 for performing a carbon dioxide (CO2) sequestration process from a gas feed stream containing carbon dioxide outputted from a power station, in accordance with a first embodiment of the present invention. With additional reference to Fig. 3, the system 10 is arranged to perform the process 100 of (i) scrubbing a gas stream containing carbon dioxide with a normal ammonium carbonate solution that is able to absorb the carbon dioxide, whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising, in the main, ammonium bicarbonate; and (ii) passing a slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| [0063] In an embodiment the method may further comprise a stage (iii) of contacting flue gases with a circulating dilute normal ammonium carbonate solution that may be chilled to the extent necessary, in a vessel in a counter-current, staged manner so thatresidual ammonia in the flue gases is scrubbed from these gases to levels low enough to allow their final discharge in the atmosphere.\| [0064] In the illustrated embodiment the stages (i) and (iii) are performed within a first apparatus 20 having separate chambers, in the form of an absorption chamber 28 and a scrubbing chamber 30, respectively. Stage (ii) occurs within a reactor either in the form of a pipeline 52 (as shown in Fig. 1) or, as will be described in more detail in subsequent paragraphs with reference to Fig. 2, an underground chamber excavated at a sufficient depth to facilitate conditions for the carbonation reactions to take place. According to Fig. 1, the pipeline 52 may connect the reactor to a mineral quarry site from with metal silicate is sourced.\| [0065] The carbon dioxide sequestration process utilised in embodiments of the present invention is based on mineral carbonation. Mineral carbonation is a reaction between a metal-oxide-bearing mineral material and carbon dioxide. The metal-oxide bearing material may, for example, be alkaline-earth metals. Advantageously, the process 100 does not require the source of carbon dioxide to be particularly pure. In mineral carbonation, carbon dioxide reacts with the metal oxide bearing material to generate insoluble carbonates, that is to say:\| [0066] MO + CO2 → MCO3 + heat (1)\| [0067] which is an exothermic reaction, occurring more rapidly at elevated temperature, typically above 1500C. Certain chemicals may serve to increase the rate at which this reaction proceeds without being consumed themselves, i.e. they serve as catalysts. The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage). Further, embodiments are inherently operable to make bicarbonate ions as carbon dioxide is absorbed into the ammonia-rich ammonium carbonate solution, without having to handle highly pressurized carbon dioxide.\| [0068] The exact nature of the insoluble carbonates formed by the reaction depends on the metal-oxide bearing material. Suitable materials may be naturally occurring alkaline-earth metal-rich silicate rocks which contain mineral constituents such asserpentine (Mg3Si2O5(OH)4), olivine (Mg2SiO4), orthopyroxene (MgSiO3), talc (Mg3Si4O10(OH)2) and wollastonite (CaSiO3). In practice, the element Iron (Fe) may substitute for some of the Magnesium (Mg) or Calcium (Ca). Other suitable materials include alkaline industry residues such as slag from steel production, the ash (both fly and bottom) from pulverised coal-fired boilers, the ash remaining from the combustion of paper recycling residues (de-inking ash), and cement. The amount of heat generated in the reaction will depend on the specific metal and on the mineral containing the metal oxide as can be seen below in the case of three natural silicates (heat values are given per unit mole of CO2 and at standard conditions (25°C and 0.1 MPa):\| [0069] Olivine\| [0070] Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 + 89 kJ moll CO2 (2a)\| [0071] Serpentine Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol" 1 CO2 (2b)\| [0072] Wollastonite\| [0073] CaSiO3 + CO2 → CaCO3 + SiO2 + 90 kJ mol l CO2 (2c)\| [0074] In the illustrated embodiments, the silicate rock comprises the mineral serpentine, Mg3Si2O5(OH)4. AU of the above minerals may be pre-treated to increase the surface area of rock that can subsequently come into direct contact with the carbon dioxide. In an embodiment, the pre-treatment involves crushing, grinding and/or milling of the mineral, as well as some mechanical classification and separation. For example, the minerals could be milled (e.g. wet-milled) in ball mills or equivalent to form a finely ground metal silicate slurry (hereafter 'silicate slurry') 36 wherein 90% of the mineral matter is finer than 40 microns. However, it will be understood that the extent of the pre-treatment is dependent upon the source and type of mineral(s) being used in the process. An example milling and transportation process flow is shown in Fig. 6.\| [0075] Again with specific reference to Fig. 1, the carbon dioxide sequestration system 10 will now be described in detail. The system 10 receives a raw flue gas mixture feed stream 32 that has been generated and subsequently emitted by a powerstation or other point source (not shown). In the embodiment described herein, the raw flue gas mixture 32 is passed though a filter 33 to remove most of the particulate matter. Suitable filters may include fabric filters, electrostatic precipitators and the like. Cleaning the raw flue gas mixture 32 may serve to minimise both the maintenance costs in downstream gas-handling equipment and the concentrations of particulates in flue gases ultimately discharged to the atmosphere. It will be understood, however, that while desirable for process reasons, it is not essential that the raw flue gas mixture 32 be cleaned of all particulates before it enters the scrubbing chamber 30. In an embodiment, the filtering process may additionally involve controlling the level of SOx and NOx that is present within the flue gas so as to adjust the pH level of the ammoniated slurry by virtue of the concentration of sulfate and nitrate ions present in it (which in turn affects the reaction rate between the silicate rocks and carbon dioxide by driving magnesium and calcium ions into solution) as will be described in detail below.\| [0076] To maximise heat recovery in the system 10, the filtered flue gas mixture is then passed through a heat exchange apparatus in the form of a heat exchanger 34 so that the sensible heat of the filtered flue gas mixture (typically at a temperature of around 135°C) is exchanged with the cooler gasses being expelled from the scrubbing chamber 30 of the first apparatus 20 and the filtered flue gas mixture is cooled to its water-vapour saturation temperature (i.e. to about 50°C). Suitable heat exchangers may include, for example, recuperative-type heat exchangers, such as the Ljungstrom rotary design as commonly used for air pre-heating in power stations.\| [0077] As mentioned in preceding paragraphs, the carbon dioxide sequestration system 10 receives a source of silicate slurry 36. According to the embodiment described herein, the silicate slurry source is located near or at the mine site from which the silicate rocks are sourced. As previously described, the silicate mineral sourced from the mine site is finely ground (e.g. by wet-milling in ball mills or equivalent to form the slurry) wherein roughly 90% of the mineral matter is finer than 40 microns or as determined to be appropriate for the proper operation of the process.\| [0078] According to Fig. 1, the silicate slurry 36 is first blended with a solution in water of normal ammonium carbonate to create an ammonia rich ammonium carbonate- metal silicate slurry (hereafter "absorbent slurry"). In the illustrated embodiment, the normal ammonium carbonate salts in solution (hereafter "circulating solution") is the solution in water of most of the normal ammonium carbonate salts accompanying thefinal metal carbonate/silica product. Specifically, according to the Fig. 1 embodiment, the circulating solution represents the overflow of a first thickener 90a of a counter- current decantation (CCD) thickener separation system 90.\| [0079] In flowing from the CCD thickener system 90 to the power station site, the absorbent slurry 47 passes through a first pressure-exchange apparatus 38. To minimise power consumption, the pressure of the absorbent slurry 47 may be increased by exchanging pressure with the final metal carbonate/silica product (hereafter 'final product'), typically to a pressure of approximately 100 Bar. hi addition, to minimise heat losses from the system 10 (and to ensure that the final product is cooled to a suitable temperature before it is emplaced in its final permanent repository), the absorbent slurry 47 passes counter-currently through a heat exchanger 40 to absorb the surplus sensible heat contained in the final product.\| [0080] According to Fig. 1, a pipeline 44 connects the first apparatus 20 to the silicate mineral quarry site and is used to transport the absorbent slurry 47 used in the sequestration process 100. As will be described in more detail in subsequent paragraphs, an alternate path 52 in the pipeline 44, in this embodiment, also serves to act as a controlled reactor in which the metal carbonation reaction largely takes place. At or near to the power station site, the absorbent slurry 47 is passed counter-currently through a second heat exchanger 46 and a second pressure-exchange apparatus 48, where the absorbent slurry 47 is cooled and reduced in pressure by exchange with the reactive slurry discharged from the first apparatus 20, before being fed directly into the scrubbing chamber 30.\| [0081] After arriving at the power station site, a residual circulating stream passes into a vessel in the form of a residual ammonia scrubber 56, in such a way that flue gases that have been stripped of most of their carbon dioxide content, pass upwards from below. There may be any number of counter-current contacting stages, depending only on the desired implementation. The residual ammonia scrubber 56 is operable such that the cleaned, largely carbon dioxide-free flue gases may leave the system with less than one part per million of ammonia, hi order to achieve such low losses of ammonia, the fluid circulating through this vessel may be cooled, even chilled, to an appropriate degree. Specifically, the fluid circulating through this vessel is comprised of the dilute aqueous phase described above (i.e. a clarified, dilute solution in water of normal ammonium carbonate), which enters the vessel and collects in the base of the residualammonia scrubber 56 from where it is circulated by pumps to the header sprays to above the uppermost of the contacting stages. It is this circulating flow that is cooled to the requisite extent, by firstly, arranging for it to flow firstly, through one or more first stage heat exchangers that are cooled by circulating water cooled in turn, in a cooling tower, and secondly, through one or more second-stage heat exchangers that are cooled in turn, by a stream of water or other suitable heat-exchange fluid that has been chilled to below ambient temperatures by a chilling plant suitable for the purpose. In an embodiment, the chilling plant is an ammonia absorption chiller 82, the operating principles of which are understood by those skilled in the appropriate art. It is to be understood however, that alternative types of chilling plant provided they have adequate chilling capacity, are equally suitable.\| [0082] Absorption chillers, including ammonia absorption chillers, require a source of heat for their operation. In an embodiment, some of this heat may be provided by the heat released through carbonation reactions as shown as equations 2a, 2b and 2c, depending on the type of silicate mineral used.\| [0083] The cooled filtered flue gas mixture passing through the heat exchanger 34 enters the scrubbing chamber 30 where the gas mixture passes upwards through deluging sprays of circulating solution entering from the residual ammonia scrubber 56 from above. When carbon dioxide is absorbed in the circulating solution, a further substantial quantity of heat is liberated, as gaseous carbon dioxide is absorbed into it, and reacts with the normal ammonium carbonate salts in the circulating solution. The reactions include the conversion of the normal ammonium carbonate (NELt)2CO3 to the bicarbonate NH4HCO3, via the reaction:\| [0084] (NFLt)2CO3 + CO2 + H2O -» 2NH4HCO3 (3)\| [0085] Normal ammonium Ammonium\| [0086] Carbonate bicarbonate\| [0087] While this will be the main reaction encountered, other reactions may equally occur in parallel including, when there is free molecular ammonia present in the scrubbing solution:\| [0088] NH3 + CO2 + H2O -> NH4HCO3 (3a)As well, some of the ammonium bicarbonate may lose some combined water to form the carbamate, NH2COONH4, hence this compound will likely be present in smaller quantities, perhaps along with some urea, CO(NH2)2, formed when the carbamate loses additional combined water.\| [0089] FURTHER DETAIL OF SEQUESTRATION PROCESS\| [0090] In more detail, the carbon capture process begins with the metal silicate (in this case, ground serpentine) being blended into a circulating solution of serpentine and an aqueous phase containing normal ammonium carbonate in solution to thereby produce the absorbent slurry. The absorbent slurry is then circulated using pumps, through a carbon dioxide absorption chamber 28 which in an embodiment may be the lower half of a tall scrubbing chamber 30 (the upper part being utilised as the residual ammonia scrubber 56). The absorption chamber 28 may, for example, take the form of a flue gas desulfurization scrubber, with the absorbent slurry circulated at high flow rates through banks of sprays.\| [0091] The absorbent slurry is heated by the transfer of latent heat from the flue gases rising from below. Also, as mentioned above, when carbon dioxide gas is absorbed into the absorbent slurry, substantial quantities of heat are liberated, as carbon dioxide reacts with the mainly normal ammonium carbonate (NHi)2CO3, to form the bicarbonate NH4HCO3, as per Equation 3 (there may also be some intermediate salts e.g. the sesquicarbonate (NFLO2CO3. NH4HCO3, the carbamate NH4COONH2, and traces of urea, CO(NH2)2). The heat of solution, along with the latent heat released when water vapour in the flue gases condenses, is removed by circulating the absorbent slurry through water-cooled heat exchangers 84.\| [0092] As mentioned above, the output from the absorption chamber 28 is a reactive solution in the form of a metal silicate slurry in an aqueous phase that is itself a solution of carbonate-rich ammonium carbonates, primarily ammonium bicarbonate. A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor.On route to the mine site, at or near to the power station, the reactive slurry is pressurised at the second pressure-exchange apparatus 48 to a high pressure of around 120 Bar (above the critical pressures of both carbon dioxide and ammonia) and also heated to at least 100°C and preferably to at least 150°C. Heating is accomplished by transferring heat from the incoming silicate slurry arriving from the mine at the heat exchanger 46, and also, if necessary, by injection of steam 54. The heat contained in the incoming silicate slurry in part originates from reactions 2(a), 2(b), and 2(c), depending on the silicate mineral involved. hi the return pipeline 52 of the pipe reactor, at temperatures below 50°C or thereabouts, most if not all of the carbon dioxide present is in the form of ammonium carbonates. When the slurry is heated to at least 100°C under pressures of at least 100 Bar, the tendency is for the various forms of ammonium carbonates in solution to decompose to molecular carbon dioxide CO2 and ammonia NH3. These remain substantially in solution in the reactive slurry under these temperature and pressure conditions. A result of this process is the partial pressure of the carbon dioxide will be particularly high, thereby serving to enhance the speed of reaction with the silicate minerals, converting them to insoluble carbonates and silica during the transit. In an embodiment, the pipeline may be 10 kilometres in length to allow adequate time for the reactions to proceed essentially to completion resulting in the metal carbonate product that contained most if not all of the carbon dioxide originally scrubbed from the power station flue gases. It will be understood that the length may vary, however, depending on the actual implementation.\| [0093] It will be apparent that a high concentration of ammonia is maintained in the slurry throughout its passage from the power station to the silicate rock mine/quarry or other emplacement site.\| [0094] When the final product in the return pipeline 52 reaches the vicinity of the mine site, as described above, the hot pressurised final product transfers its sensible heat via the heat exchanger 40 to the absorbent slurry being pumped towards the power station, hi the process the final product is cooled to a temperature below 50°C. To achieve this temperature in practice, it may be necessary to employ additional cooling to ensure that the temperature of the final product stream is cool enough for the recombination reactions to occur. In an embodiment, the additional cooling is accomplished by means of a heat exchanger cooled by circulating cooling water fromdry (e.g. radiator-type) cooling towers, fin fan coolers, or a natural-draft cooling tower (not shown) such as used for cooling in the power station. A consequence is that free molecular ammonia and carbon dioxide will subsequently re-combine to form ammonium carbonate salts dissolved in the aqueous phase that can be recovered and used in the circulating solution. Since carbon dioxide has been removed from the aqueous phase by reaction with the mineral silicate, the ratio of carbon dioxide to ammonia is lower than it was before the key carbonation reactions occurred. Hence, the predominant form of ammonium carbonate salt formed is normal ammonium carbonate (NKU)2CO3 which, it will be noted, may contain twice as many ammonia units pre carbon dioxide unit as the bicarbonate, NH4HCO3. This is the reason why a solution rich in normal ammonium carbonate may also be referred to as an ammonia-rich ammonium carbonate solution. In any case, it will be understood that other ammonium salts, plus molecular ammonia NH3 and ammonium hydroxide NH4OH, may also be present.\| [0095] FURTHER DETAIL OF SEPARATION SYSTEM\| [0096] As previously mentioned, the final reacted slurry (i.e. containing mainly normal ammonium carbonate in solution together with the carbonate/silica solids that are the products of carbonation) is passed through a solids-liquids separation process. The separation process generally involves producing a clear overflow solution containing most of the ammonium salts and other soluble chemicals (including any molecular ammonia and ammonium hydroxide NH4OH that are dissolved in it) and a dense slurry or even paste-consistency underflow containing all of the solids.\| [0097] Separation may be accomplished by one or more of several means known to those skilled in the art. In an embodiment, a filtration process may be employed using, for example, rotary vacuum filters. In an alternative embodiment, the filtration process may use plate and frame-type filter presses. In both embodiments, a filter cake is formed on a filtration medium (a filter cloth for example) and wash-water is sprayed onto, or otherwise caused to pass through, the filter cake to wash out residual quantities of soluble materials including ammonium carbonate salts. The filter cake represents the first, solids-rich stream, which may be handled as a cake, or converted to a dense slurry by addition of small quantities of additional water sufficient to allow it to be handled asa slurry. The aqueous phase, including wash-water passing through the filter cake and filtration medium, represents the second stream. In another embodiment, separation of the solids from the aqueous phase (specifically, the separation of the ammonium carbonate salts and other soluble materials in the aqueous phase) is achieved by a process known as counter-current decantation (CCD), as illustrated in the Fig. 1 and 2 embodiments. This technique involves utilising a number of continuous thickener tanks (in the illustrated embodiment three tanks are used, although it will be understood by persons skilled in the art that more or less thickener tanks may be employed depending on the desired implementation) that are arranged in a series. The CCD thickener system 90 may recover a substantial amount (e.g. around 99 per cent) of all of the dissolved salts and other soluble substances (including ammonia) in the aqueous phase accompanying the final product. The remaining amount of salts will accompany the final product solids as they are pumped to their final permanent repository.\| [0098] It is noted that in some implementations, only a certain percentage (e.g. 80%) of soluble substances may be recovered by the first thickener 90a of the CCD system 90, with the remainder recovered by subsequent stages. In an embodiment, as shown in Figure 1, the two aqueous-phase streams resulting from the overflows of the first-stage and second-stage thickeners are blended either by arranging for the overflow of the second stage thickener to be blended with the feed stream to the first-stage thickener, or by directly blending the two overflow streams.\| [0099] In more detail, the final products stream from the reactor, after pressure reduction in the pressure exchangers 38 and cooling in the heat exchangers 40, enters the first thickener 90a of the series. The insoluble solids (the carbonated mineral) suspended in the feed stream settle in the thickener tank 90a to form a dense slurry that is withdrawn as an underflow stream. The balance of the feed entering the thickener tank overflows as a clarified supernatant, which contains most of the soluble ammonium carbonate salts and other soluble materials (i.e. the circulating solution). The underflow may still contain around 10 per cent of the aqueous phase that first entered the thickener, and it is the function of the balance of thickeners in the CCD system to recover these salts to the maximum practicable extent, from the insoluble solids that are to be finally emplaced. In the CCD system 90, the underflow slurry from thickener tank 90a is pumped to the next thickener tank 90b in line. Also fed to tank 90b is the clarified overflow from thickener tank 90c, and so on. Where "N" thickenertanks are employed, the final thickener tank in the series, tank N, receives a feed stream which is a mixture of the underflow of thickener tank N-I, and fresh water, which may be replaced in part by any surplus aqueous phase recovered from final emplacements of carbonated mineral as this further consolidates and/or drains from the mineral, over time. In an embodiment, a mixture of thickener tanks, one or more stages in series, and filtration units may be used to effect the separation of soluble ammonium carbonate salts from the insoluble carbonated mineral.\| [0100] The dense slurry stream (in one embodiment a filter cake, in another embodiment the underflow of CCD thickener Unit N) is the final product slurry substantially free of salts, and in a form suitable for permanent emplacement in mine voids or other purpose-built repositories (not shown). In these emplacements the solids can settle and consolidate, releasing additional aqueous phase as a clear supernatant. This supernatant may also be collected and re-used in the process, as described in the paragraph above. When the CCD system 90 for the recovery of ammonium salts is close to the power station, as may be the case for the underground chamber reactor embodiment (Fig. 2), it may be appropriate to add the remainder of the power station fly ash to the final product slurry from the carbon sequestration process, so the two streams may be handled and co-disposed of as a single stream. An advantage stemming from the presence of fly ash having pozzolanic properties (a tendency to "set" in the presence of alkalis and moisture) in the final product, is that it will assist with the rehabilitation process, by encouraging the final product/fly ash mix to "set", thereby immobilising the contents of the emplacement. hi an embodiment the overflow of the second stage of the CCD thickener system 90, being a relatively dilute, clarified (insoluble solids- free) solution in water of ammonia-rich ammonium carbonate salts may be handled separately (see Fig. 2). hi such an embodiment, the stream (hereafter "residual stream") is sent overland from the CCD system 90 (installed near the silicate quarry) to the power station site via a separate, third pipeline 91. Pumps raise the pressure of the contents of the third pipeline 91 to the extent necessary for them to traverse the length of the pipeline 91. However, it will be understood that the third pipeline 91 may be configured to accept some of the heat and some of the pressure energy released when the pressure and temperature of the final products pipeline are reduced via heat- and pressure-exchange equipment.Whether the third pipeline 91 is configured in this way, or simply used as a conduit for the return of this stream to the power station site, depends on the individual circumstances of the installation.\| [0101] 5 CHEMICAL REACTIONS\| [0102] The main chemical processes occurring throughout the process are as follows: 3CO2 + 3(NH4)2CO3 + 3H2O -» 6NH4HCO3 (4)\| [0103] 6NH4HCO3 -> 6NH3 + 6H2O + 6CO2 (5)\| [0104] 6CO2 + Mg3Si2O5(OH)4 -» 2SiO2Φ + 3MgCO3Ψ + 2H2O 0 + 6NH3 + 3CO2 (6)\| [0105] 3CO2 + 6NH3 + 3H2O -» 3(NILO2CO3 (7)\| [0106] NH3 + NH4HCO3 -» (NILO2CO3 (8)\| [0107] Equation 4 represents the absorption of carbon dioxide into the ammonia-rich5 ammonium carbonate aqueous phase to produce a solution comprising ammonium bicarbonate. On heating under pressures of at least 100 Bar in the reactor (i.e. pipeline or underground chamber), this ammonium bicarbonate decomposes to molecular ammonia, water and carbon dioxide according to equation 5. As shown in equation 6, under the high pressure and temperature conditions prevailing in the reactor the carbon O dioxide reacts with the serpentine (the chemical formula of which is shown in equation 6) or other silicate rock to form insoluble metal carbonates and silica, the final products of the process, which store the carbon dioxide. Equation 7 describes what happens after the reaction products are cooled to below 50°C, i.e. low enough to allow the free molecular ammonia and carbon dioxide to combine to form ammonium carbonate salts5 in solution. As shown, since much of the carbon dioxide has been absorbed by the metal silicate (here serpentine) the ratio of ammonia to carbon dioxide favour formation of the ammonia-rich normal carbonate. Additional normal ammonium carbonate may form according to equation 8, by reaction between ammonium bicarbonate, and free molecular ammonia. 0CONTROLLING ACIDITY IN THE SYSTEM\| [0108] As mentioned in preceding paragraphs, sulfate ions from SOx, and nitrate ions from NOx respectively, contained in the raw flue gases, may accumulate in the circulating solution of ammonium salts. Oxides of sulfur (SOx) are inevitable byproducts of the combustion of fossil fuels including coal, that incorporate sulfur- containing compounds in reduced form, for example pyrite (iron disulfide FeS2). Oxides of nitrogen (NOx) are also inevitable byproducts of the combustion of fossil fuels including coal, originating from nitrogen-containing compounds in the fuel, and from reactions between oxygen and nitrogen in air induced by the heat of the fuels' combustion, hi an Australian context, where coals tend to have low sulfur contents, and assuming use of modern "low-NOx burners", the rates of build-up of nitrate ions will not be high, but their build-up may still need to be limited to maintain the pH range to that most suited for the overall processes. When the SOx and NOx contained in flue gases contact the absorbent slurry as encountered in the scrubbing chamber 30 in the presence of additional oxygen including that contained in flue gases, a series of reactions occur that convert these gases to sulfates and nitrates: SOx to sulfate ions SO4— , and NOx to nitrate ions NO3-. In the normal course of separating out the insoluble solids for example magnesite and silica formed from the reactions between carbon dioxide and the metal silicates, as previously described, the soluble salts dissolved in the aqueous phase from the reactor including sulfates and nitrates are recycled for re-use in the scrubber, apart from the small quantities of such salts that are ultimately emplaced with the final product metal carbonates and silica. A consequence is that while carbon dioxide entering the system forms additional carbonate ions that are ultimately removed at an equal rate as insoluble metal carbonates, the tendency is for both sulfate and nitrate ions to accumulate in the circulating aqueous phase. In an embodiment, the system may implement a process for limiting the build-up of these ions (anions) to avoid an increase in the acidity (reduction in the pH number) of the circulating solution, as the formation of these ions leads to a concomitant formation of hydrogen ions in solution. It is noted that the system, to some extent, may inherently limit such a build-up by virtue of the fact that, as mentioned in the previous paragraph, not all soluble salts and other dissolved substances will be recovered by way of the solids-liquids separationprocess. To further reduce nitrate ion equilibrium concentration, it is necessary to limit correspondingly, the concentrations of NOx gases in the flue gases entering the scrubbing vessel 30. This may be achieved, for example, by using so-called 'low-NOx burners', and by other methods which achieve control of the combustion process to limit NOx formation in the power station's boilers.\| [0109] To control concentrations of sulfate ions in the circulating aqueous phase, the system 10 may employ an additional control mechanism 96 arranged to add/feed appropriate quantities of calcium oxide or hydroxide (which in water form calcium ions and hydroxyl ions) to a portion of the circulating slurry (a side-stream), wherein the sulfate ions react with it to form calcium sulfate, which mostly precipitates out as the sparingly soluble hydrated salt, gypsum:\| [0110] SO4" + Ca+* + 2H2O -» CaSO4.2H2O Ψ (9)\| [0111] Meanwhile, the hydroxyl ions combine with and neutralise a corresponding number of hydrogen ions (to form water molecules), thereby controlling (reducing) the acidity of the circulating solution.\| [0112] In an embodiment, calcium oxide generally may be naturally present in the power station fly ashes. If present in sufficient concentrations, the appropriate quantities of fly ash may be added by the control mechanism 96 to the circulating solution to control the pH levels to the desired ranges. If the quantities of calcium oxide naturally present in fly ash are inadequate, they may, in an embodiment, be augmented by adding pulverised limestone to raw power station flue gases in the boilers at one or more locations for example immediately upstream of the economiser section of the boilers, where flue gas temperatures are appropriate for the decomposition of limestone to calcium oxide and carbon dioxide (when exposed to furnace temperatures of 1,0000C or more, limestone is calcined to quicklime.\| [0113] Treatment processes applied to this side stream may also incorporate steps to recover base metals and other valuable components in solution, including nickel, copper and iron, hi one form, side-stream treatment may involve adding an inexpensive alkali, e.g. calcined lime, dolomite, limestone or the like. Sulfate ions can be removed via the following equation (shown for normal ammonium sulphate and calcium oxide):(NILt)2SO4 + CaO + 3H2O -» CaSO4.2H2θΨ + 2NH4OH (10) ammonium quicklime gypsum ammonium\| [0114] Sulfate hydroxide\| [0115] In an embodiment the control mechanism 96 may be further arranged to add fresh ammonia to the circulating solution, at an appropriate rate, to account for any losses of ammonia.\| [0116] FURTHER DETAIL OF ABSORPTION/SCRUBBING CHAMBER OPERATION Conditions in the absorption chamber 28 may be strongly oxidising to assist the conversion of the impurity gases dissolving in the aqueous phase of the slurry (i.e. SOx ending up as sulfates rather than sulfites, and NOx ending up as nitrates rather than nitrites). In an embodiment, the cool, saturated condition of the flue gases when in the absorption chamber 28, plus the partial pressure of oxygen in these gases of three per cent or more, may be sufficient to ensure oxidising conditions. As well, the large pool of slurry held in the bottom of the absorption chamber 28 may be aerated using compressed air as is normal practice with flue gas desulfurisation (FGD). However, if additional oxidising is required, the process may further involve irradiation of the flue gases immediately upstream of their entry into the absorption chamber 28 by electron beams or high- voltage brush discharge, to form free radicals from water and oxygen (OH" and 0~). These are powerful oxidising agents, able to convert rapidly, sulfur dioxide SO2 to the trioxide SO3, and nitric oxide NO to the dioxide NO2, the precursors to sulfates and nitrates respectively. Thus, the absorption chamber 28 may serve as a highly efficient scrubber for the removal of SOx and NOx. It may also remove volatile metals that may exist in trace quantities in coal and that end up in flue gases notably mercury (the low operating temperatures and oxidising environment will tend to favour the conversion of any mercury vapour present to non- volatile mercuric oxide, an insoluble solid that will accompany the final product metal carbonate and silica to their permanent emplacement).\| [0117] FURTHER DETAIL OF PRESSURE EXCHANGERS\| [0118] With reference to Fig. 4, there is shown an arrangement for the pressure- exchange apparatus described above. At the end of the reaction process, the pressure ofthe final carbonate-rich product must be reduced from approximately 120 Bar to atmospheric pressure. Instead of merely reducing pressure by throttling valves, thereby losing the energy embodied in this pressure, the energy this pressure represents may be conserved by transferring it to the extent possible, to the silicate slurry. In Fig. 4, slurry A comprises the products of the reactions that occur as the ammoniated, carbonated silicate slurry flow through the pipeline 44 from the power station to the mine site; while slurry B represents silicate slurry from the mine. A consequence of pressure exchange in these two stages is that slurry A's pressure would fall from around 120 Bar to near ambient pressure, while that of slurry B would rise from around atmospheric pressure to perhaps 100 Bar.\| [0119] Another pressure-exchange apparatus is also utilised at the power station site. Here, using the terminology of Fig. 4, slurry A represents the hot silicate slurry arriving via the pipeline from the mine; while slurry B comprises slurry exiting the scrubbing chamber 30 (i.e. silicate slurry now charged with ammonia and carbon dioxide, but at close to ambient pressures). A consequence of pressure exchange in this stage is that slurry A's pressure would fall from its arrival pressure (this may be 120 Bar, a pressure that would be maintained by booster pumping stations at strategic locations along the pipeline 44 to overcome friction losses), to near ambient pressure. This pressure may be transferred (exchanged) to the extent possible to slurry B, thereby minimising the amount of pumping energy required to raise the pressure of this slurry to the levels required, here assumed to be 120 Bar. Since slurry A at this point will be at well below 120 Bar, pressure-exchange between slurries A and B alone may not be capable of raising the pressure of slurry B to 120 Bar. Also, the volume of slurry B may exceed that of slurry A. This is because of the much higher contents of carbon dioxide and ammonia, and of water condensed out of the power station flue gases. In an embodiment, additional pumping capacity may be installed to boost slurry B pressures to those required for the pipeline 44, and to pressurise those (relatively small) quantities of slurry B that cannot be pressurised by pressure-exchange with slurry A. For this function, conventional high-pressure diaphragm pumps, such as the Geho pump manufactured by Weir Netherlands b.v., may be implemented. This pumping, together with the pumping energy required to maintain pressures along the length of the pipelines, account for a substantial proportion of the total mechanical energy input to the total process. Other suitable pressure exchange/pump-turbine sets may comprisecentrifugal pumps and radial-type hydraulic turbines. As the pressures are relatively high, the type of centrifugal pump may be a multi-stage barrel-type pump.\| [0120] With reference to Fig. 5 there is shown a configuration for the heat exchanger arrangements 40 & 46, according to an embodiment of the present invention. As previously discussed, high temperatures are required to initiate and accelerate the carbon sequestration reactions: the conversion of metal silicates to carbonates. These reactions, being exothermic, yield additional heat that can and should be applied to assist with creating the conditions needed for these reactions to proceed most efficiently. As shown, the heat-exchanger arrangement is in the form of a simple shell- and-tube heat exchanger, consisting of two concentric pipes: the inner forms the "tube", the outer, the "shell". An advantage with this arrangement is that the heat exchanger can be made as long as is required to affect the desired transfer of heat: if necessary, many hundreds of metres long. For heat exchanger 40 (i.e. the heat exchanger on the silicate rock quarry site side), heat energy is transferred between the final carbonate/silica product (i.e. slurry A), which is hot, and the silicate slurry (slurry B), which is cool. For heat exchanger 46 (i.e. the heat exchanger on the power station side), slurry A would be hot silicate slurry from the quarry, while slurry B would be slurry exiting the scrubbing chamber 30 (i.e. now charged with ammonia and carbon dioxide, but at close to ambient temperatures).\| [0121] UNDERGROUND REACTOR\| [0122] Turning now to Fig. 2, there is shown an alternative system 200 for performing carbon dioxide sequestration which utilises (where geological conditions permit) an underground chamber as the reactor, as opposed to a pipeline reactor as illustrated in Fig. 1. In this embodiment, the reactor is in the form of a chamber 70 excavated from bedrock at a depth sufficient to allow the conditions for the core carbonation reactions to be generated entirely or partly by static head alone (e.g. 100 Bar). A chamber 70 excavated at a depth of approximately 800 meters and having a volume of 300,000 cubic meters, sufficient to allow for a 24 hours' detention time for the contents, may be envisaged for holding the reactive slurry output from a system 200 fitted to an efficient\| [0123] 1,000MWe coal-fired power station. In practice a smaller chamber may suffice, should it arise that the reactions are essentially completed in less time.\| [0124] The silicate slurry 36 may be prepared either at the serpentine quarry site andpumped overland to the power station site, or, the mineral could be railed, trucked or otherwise suitably transported to the power station site, and prepared there. Were the former implementation adopted, pipeline arrangements 44 would be considerably simpler than for the pipeline reactor embodiment described above with reference to Fig. 1. Specifically, the silicate slurry 36 would not be required to collect and transport heat and pressure energy from the quarry site to the power station site, nor to host any residual ammonium salts. The pipeline 44 would simply be utilised for mineral transport; whether it was transported as a lump product by rail or as slurry by pipeline would be determined by economic and environmental considerations. It will be appreciated that in this embodiment, silicate slurry density may be substantially higher (e.g. 60 per cent solids by weight), thereby reducing the volumes of silicate slurry required to be pumped, and allowing a lower pipeline velocity because of the reduced tendency for the solids in denser slurries to segregate and silt up the pipeline 44. Also, arrangements for conserving heat and pressure are much simpler than they would need to be for the pipeline reactor alternative.\| [0125] In Fig. 2, an injection pump 72 is utilised to drive the circulation of the reactive slurry from the scrubbing chamber 40, through a plurality of counter-current heat exchangers 74, 76, underground reactor 70 and counter-current decantation system for the separation of normal ammonium carbonate and other salts in the aqueous phase of the products of the underground reactor, and the insoluble carbonated mineral solids that are to be emplaced permanently.\| [0126] Heat exchangers 74, 76 are shown in schematic form at two locations on Fig. 2. The heat exchangers 74, 76 may be long, shell-and-tube designs, as shown in Fig. 4: they may span most of the vertical distance from the scrubbing chamber 40 down to the underground chamber 70. This is to say, whereas two separate pipelines are implied in Fig. 2, in practice, for most of their length they may be concentric: the annulus formed between the outer and concentric inner pipe transporting the hot reaction products, while the inner pipe transports the products heading downward to the Reaction chamber. It will be understood by persons skilled in the art that this selection may be reversed.\| [0127] In contrast to the pipeline reactor configuration shown in Fig. 2, heating of the reactive slurry may be accomplished by exchanging heat from the hot reaction productsrising first from the ammonia gas recovery vessel 78, and as the raw slurry descends further, from hot slurry rising from the underground chamber 70. While some supplementary heat may be required, the heat generated by Equation 2(b) would be conserved, and available to heat raw reactive slurry. The design of the underground chamber 70 may be optimised to achieve some plug- flow characteristics. In an embodiment, the chamber 70 may have a high length- to-diameter ratio of 10: 1 and be vertically aligned. Utilising a vertically aligned chamber provides that the incoming reactive slurry, being cooler hence slightly denser than the average contents of the reactive chamber 70, will tend to stratify at lower levels, displacing hotter slurry upwards. In an embodiment, the underground chamber 70 may be subdivided into two or more vertically stacked sub-chambers.\| [0128] In an embodiment, the reactive chamber 70 may employ an agitator (not shown) to maintain the solids in suspension. This may be advantageous where large residence times are required, implying in turn large reactor volumes. As will readily be appreciated, heat losses from the underground chamber 70 and pipelines may be much smaller than they would be even from a lagged above- ground pipeline and may be further reduced by insulation surrounding the reactor, pipelines and any other underground process vessels. Whereas an overland pipeline represents a plug-flow reactor, ideal conditions for a relatively slow series of reactions as are involved in carbon sequestration are also obtained in the embodiment illustrated in Fig. 2.\| [0129] It is noted that in the Fig 2 embodiment, the two overflow streams from the CCD system are handled separately. The overflow of the first thickener tank 90a is blended with the silicate slurry 36, incoming from the quarry site to form the circulating solution to be sent to the absorption chamber 28.\| [0130] The balance of the process in relation to sequestration, separation and emplacement is as for the overland pipeline reactor case.Example\| [0131] Again with specific reference to Fig. 3, a non-limiting example process flow for carbon sequestration for the first system configuration 10 described herein (i.e. the system depicted in Fig. 1) will now be given, wherein for convenience, like parts to those shown in the foregoing embodiment have been numbered with like numerals.\| [0132] Example 1\| [0133] Table 1: Indicative mass balance figures from 1.000 MWe of black coal-fired electricity generation plant. Material Per year Per hour\| [0134] Total CO2 generated: 6.4 m. tonnes 80O t\| [0135] (NKU)2CO3 to absorb 90% of this CO2 1,60O t\| [0136] Resulting quantity OfNH4HCO3 formed 2,400 1\| [0137] Water to make up 25% solution OfNH4HCO3 7,200 t Serpentine to absorb 90% of this CO2, 80% eff. 17.2 m tonnes 2,150 t\| [0138] Total slurry with NH4HCO3: 9,350 t\| [0139] Slurry density: 1.2 t/m3 1.2 t/m3\| [0140] Slurry volume, m3 8,000 m3\| [0141] Product (carbonate plus silica) solids: 20.6 m. tonnes 2,600 1 Slurry pipe dia. with 3 m/s velocity: 1.0 metres 1.0 metres\| [0142] Ammonia lost due to SOx (90% recovery via Eq. 10) ) 11,,66000O 1t 0.2 t\| [0143] Ammonia lost due to NOx 3,0001 0.37 t\| [0144] Total losses of ammonia: 4.600 1 0.57 t\| [0145] Table 1 provides an indicative detailed mass balance for a carbon dioxide sequestration process, assuming:\| [0146] - 90 per cent carbon dioxide capture and sequestration from 1,000 MWe of black coal- fired electricity generation plant, which when operating in base-load mode might expect to generate annually 8,000 GWh of electricity; - where on a dry ash-free basis, the coal is 81.3% by weight carbon and 0.65% sulphur (as S) and the flue gases contain 400 ppm NOx.An advantage of the carbon dioxide sequestration process 100 and systems 10, 20 according to embodiments of the present invention is that by selecting ammonia as a catalyst/promoter, a single integrated process can be provided for both capture and sequestration of carbon dioxide. In an embodiment, sequestration of the carbon dioxide takes place in a reactor, in the form of a return pathway 52 of a pipeline 44, which advantageously connects the power station (i.e. the source of carbon dioxide) to the source/destination of the absorbent material being used in the process, hi an alternative embodiment, where geological conditions permit, the reactor may take the form of an underground chamber which advantageously facilitates the reaction without requiring pressure-exchange and head-recovery equipment required for the pipeline embodiment. Another advantage of the carbon dioxide sequestration process and systems is that the reaction kinetics may be improved by using ammonia. Therefore, by using ammonia and exploiting the heat generated by the exothermic reaction, the energy consumption of the process 100 can be kept to a minimum. As the reaction products are thermodynamically stable, carbon dioxide can be stored in a permanent stable solid form. Following from this, further advantages include lower operating and capital costs.\| [0147] Persons skilled in the art will appreciate that further advantages may arise from carrying out certain steps of the aforementioned embodiments in isolation. For example, the catalytic effect of a solution of ammonia with an ammonium salt (that may be ammonium carbonate formed by exposing an ammonia-rich solution to a gas stream containing carbon dioxide) in the carbon dioxide sequestration process can also be utilised for extracting metals (e.g. magnesium, iron, nickel, copper and other metals present in the silicate rock) from metal silicates, such as magnesium-rich metal silicates. In such an embodiment a solution of ammonia-rich ammonium carbonates in water may be mixed with a metal silicate (typically in slurry form) to allow the dissolution of magnesium ions by ammonia to recover the metal, in this embodiment a metal compound in the form of magnesium carbonate. The mixing may occur in an ammonia absorption chamber such as that previously described in connection with the preceding embodiments. Preferably the solution contains molecular ammonia in the presence of ammonium salts in solution, such as ammonium carbonate, to prevent the precipitation of magnesium hydroxide, hence allowing the dissolution of magnesium ions by ammonia to continue, substantially free of concerns over tendencies for otherwiseinsoluble magnesium hydroxide to coat, and restrict access to the silicate mineral by carbon dioxide and ammonia. A further advantage arising from this process is that after extraction of magnesium carbonate, other minerals (metals) present within the silicate rock are also amenable to recovery. The silicate rock may comprise mafic or ultra- mafic rocks (i.e. rocks with respectively a high or very high ratio of magnesium to silicon content).\| [0148] Expressed another way, the catalytic effect of the ammonia follows from its tendency to form complexes (ammines) with certain metal ions including magnesium (Mg2+), divalent iron (Fe2+), copper (Cu2+) and nickel (Ni2+). The presence of ammonium salts notably the various carbonates formed from the reaction between ammonia and carbon dioxide prevents precipitation of the otherwise insoluble magnesium hydroxide. Magnesium carbonate is however insoluble in such an environment, so a precipitate of this compound will form from the reaction between magnesium hydroxide and ammonium carbonate, to yield ammonium hydroxide and free molecular ammonia in solution, the latter continuing to extract additional magnesium and other metals from the silicate rock through formation of ammine complexes until all such susceptible metals have been extracted.\| [0149] Finally, it is to be appreciated that various alterations or additions may be made to the parts previously described without departing from the spirit or ambit of the present invention. The process is not limited to having a single two-stage continuous reactor, or a single tube-like reactor, as the process may be arranged to utilise alternatively configured items of equipment as necessary to accommodate process variables, arising from different source materials, capital and operating costs. For example, in the exemplary embodiment previously described the plant design is based on the emission of 800 tonnes CO2/GWh generated from a state-of-the-art black coal- fired electricity generation plant. By comparison, the Bayswater Power Station and the Liddell Power Station, both in the Hunter Valley of New South Wales, Australia, able to generate 2,640 MWe and 2,040 MWe respectively, being older hence less efficient can be expected to emit between 850 and 900 tonnes CO2/GWh. Thus the concentration and rate of carbon dioxide emissions in the flue gas emitted by the power plant may vary such that the plant equipment design may be reconfigured to accommodate these variables. For example, alternative equipment can be configured for the various heat and pressure exchange stations. The carbon dioxideabsorption zone and the scrubbing zone may be arranged in series in two separate vessels (rather than the nested configuration shown in Fig. 1). The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s). As well, the corresponding solids concentration in the slurry feed may be higher or lower than 25% solids by weight. It is possible that the metal silicate solution may comprise a blend of metal silicates, e.g. mixture of serpentines and olivines, even pyroxenes. The reaction kinetics may require heat to be removed from the reactive solution (rather than heat addition as described above). These factors will impact and alter the system pressures. There might be two or more pipelines for transporting the metal silicate solution and the reactive solution; because there are more pipelines, additional heat exchangers and pressure-exchange apparatus may be used. The power station flue gas may include additional pre-processing steps including flue gas desulphurisation (FGD) and selective catalytic reduction (SCR) to reduce concentrations of SOx and NOx respectively hence losses of ammonia from the system. Furthermore, the availability of services, such as steam and cooling water may require different equipment arrangements.\| [0150] Any reference to prior art contained herein is not to be taken as an admission that the information is common general knowledge, unless otherwise indicated.\| [0151] In the claims which follow and in the preceding description of the invention, except where the context requires otherwise due to express language or necessary implication, the word "comprise" or variations such as "comprises" or "comprising" is used in an inclusive sense, i.e. to specify the presence of the stated features but not to preclude the presence or addition of further features in various embodiments of the invention.	Family Number\|(1878278)\|1878278\|Object of Invention\|(AU2010210311 A1)\| (...) absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock\|3 0 In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of: (i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium (...) ammonium carbonate to produce a solution comprising ammonium bicarbonate; (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\|(CN102395417 A)\|In a first aspect , the present invention provides a method for sequestration of carbon dioxide comprising the steps of : \|The present invention provides a carbon dioxide capture and sequestration process comprising a first stage of scrubbing a carbon dioxide containing gas stream with a solution containing normal ammonium carbonate capable of absorbing carbon dioxide , wherein the carbon dioxide reacts with the ammonium ( . . . ) \|The present invention relates generally to systems , devices and methods for carbon dioxide sequestration , and more particularly , but not exclusively , to systems and methods for capturing and sequestering carbon dioxide from flue gases of coal - fired power plants . \|(WO201088738 A1)\|Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\|hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and (...) In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|(IN2011DN06815 A)\|Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from coal-fired power station flue gases.\|hi accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and (...) In accordance with a fourth aspect the present invention provides a method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|Abstract\|(AU2010210311 A1)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|(CN102395417 A)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate . In a second stage , a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica . \|(EP2393577 A4)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|(WO201088738 A1)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|(IN2011DN06815 A)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate.In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\|Title\|(AU2010210311 A1)\|System, apparatus and method for carbon dioxide sequestration\|(CN102395417 A)\|System , apparatus and method for carbon dioxide sequestration \|(EP2393577 A4)\|System, apparatus and method for carbon dioxide sequestration\|(EP2393577 A1)\|System, apparatus and method for carbon dioxide sequestration\|(WO201088738 A1)\|System, apparatus and method for carbon dioxide sequestration\|(IN2011DN06815 A)\|System, apparatus and method for carbon dioxide sequestration\|(HK1164777 A)\|System, apparatus and method for carbon dioxide sequestration\|Advantages / Prev. Drawbacks\|(WO201088738 A1)\|The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage).\|(IN2011DN06815 A)\|The inventor of the present invention has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration into a stable mineral form (storage).\|Independent Claims\|(AU2010210311 A1)\|1. A carbon dioxide sequestration process including the steps of: (...) (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| (...) absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|36. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|(CN102395417 A)\|1. A method of carbon dioxide sequestration comprising the steps of : ( . . . ) ( ii ) passing a reaction slurry comprising metal silicate rock and an ammonium bicarbonate solution through a reactor , the reactor being controlled so as to promote a reaction between the ammonium bicarbonate and the silicate rock to produce metal carbonate and silica . \|( . . . ) ( b ) a reactor for receiving a reaction slurry comprising metal silicate rock and ammonium bicarbonate produced by ( a ) , the reactor being controlled so as to promote a reaction between the ammonium bicarbonate and the metal silicate to produce a metal carbonate and silica . \|38. Providing a first fluid channel in the pipeline , the first fluid channel transporting a metal silicate slurry for use by a first apparatus in a carbon sequestration process ; and a second fluid passageway that carries the reacted ammonium bicarbonate - metal silicate slurry from the first apparatus , wherein the second fluid passageway is controlled so as to promote reaction of the bicarbonate with the metal ( . . . ) \|39. A process for reacting a slurry comprising metal silicate rock and an aqueous phase comprising an ammonium bicarbonate solution to produce a metal carbonate , the process comprising the steps of : \|(WO201088738 A1)\|1. A carbon dioxide sequestration process including the steps of: (...) (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| (...) (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|38. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and (...) \|39. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|(IN2011DN06815 A)\|1. A carbon dioxide sequestration process including the steps of: (i) scrubbing a gas stream containing carbon dioxide with a solution rich in normal ammonium (...) ammonium carbonate to produce a solution comprising ammonium bicarbonate; (ii) passing a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.\| (...) absorbing it in a normal ammonium carbonate solution whereby the carbon dioxide reacts with the normal ammonium carbonate to produce a solution comprising ammonium bicarbonate; and (b) a reactor for receiving a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate resulting from (a), the reactor being controlled so as to promote the reaction between the bicarbonate and the metal silicate to produce a metal carbonate and silica.\|38. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive ammonium bicarbonate-metal silicate slurry from the first apparatus, wherein the second flow path is controlled so as to encourage the bicarbonate to react with the metal silicate and (...) \|39. A method for causing a slurry consisting of metal silicate rock and an aqueous phase comprising ammonium bicarbonate in solution, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the (...) \|	Chemical engineering\|Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-053/77\|B01D-053/96\|B01D-2251/206\|B01D-2251/606\|B01D-2257/504\|C01B-032/60\|Y02C-020/40\|Y02P-020/151		B01D-053/62\|B01D-053/77\|B01D-053/96\|B01D-2251/206\|B01D-2251/606\|B01D-2257/504\|C01B-032/60\|Y02C-020/40\|Y02P-020/151	B01D\|B01D-053/62\|B01D-053/96\|C01B\|C01B-032/50\|C01B-032/60	B01D\|B01D-053/62\|B01D-053/96\|C01B\|C01B-031/20\|C01B-031/24			WO2024208737\|EP4442351\|WO202444690\|EP4353956;EP4353956\|EP4051414;EP4051414\|CN111715146\|CN108710778\|CN108031242\|CN107021488\|WO201599612\|CN103974757\|EP2763783;EP2763783\|WO201349896\|DE102024201178\|EP4359113\|DE102021116491\|US12409413\|CN108139502B\|US9896741\|WO201228418\|CN102114383B\|CN102078743B	WO2024208737 111711345 WHO=Examiner SELF=N CAT=X CAT=I\|EP4442351 111711345 WHO=Examiner SELF=N CAT=X CAT=I\|WO202444690 108683267 WHO=Examiner SELF=N CAT=A\|EP4353956 98745634 WHO=Examiner SELF=N CAT=A\|EP4051414 93920984 WHO=Examiner SELF=N CAT=A\|CN111715146 90806865 WHO=Examiner SELF=N CAT=A\|CN108710778 81767099 WHO=Examiner SELF=N CAT=A\|CN108031242 79710421 WHO=Examiner SELF=N CAT=A\|CN107021488 75106585 WHO=Examiner SELF=N CAT=A\|WO201599612 69805816 WHO=Examiner SELF=N CAT=A\|CN103974757 44920168 WHO=Examiner SELF=N CAT=A\|EP2763783 44920168 WHO=Examiner SELF=N CAT=A\|WO201349896 44920168 WHO=Examiner SELF=N CAT=A\|DE102024201178 115623811 WHO=Examiner SELF=N\|EP4359113 103205323 WHO=Examiner SELF=N\|DE102021116491 103205323 WHO=Unknown SELF=N\|US12409413 93920984 WHO=Applicant SELF=N\|CN108139502B 76398916 WHO=Examiner SELF=N\|US9896741 69805816 WHO=Applicant SELF=N\|WO201228418 18771696 WHO=Applicant SELF=N\|CN102114383B 7351345 WHO=Examiner SELF=N\|CN102078743B 7290484 WHO=Examiner SELF=N	AU2008217572\|AU2008217572\|WO2008101293\|WO200760149\|WO200760149\|US20080031801\|US20080031801\|CN101010129\|CN1153482	AU2008217572 6597398 WHO=Examiner SELF=N CAT=X\|AU2008217572 6597398 WHO=Examiner SELF=N CAT=X\|WO2008101293 6597398 WHO=Examiner SELF=N CAT=X\|WO200760149 5345427 WHO=Examiner SELF=N CAT=A\|WO200760149 5345427 WHO=Examiner SELF=N CAT=A\|US20080031801 43690578 WHO=Examiner SELF=N CAT=A\|US20080031801 43690578 WHO=Examiner SELF=N CAT=A\|CN101010129 76566186 WHO=Examiner SELF=N CAT=A\|CN1153482 1355390 WHO=Examiner SELF=N CAT=A		AU2008217572; US20080031801; WO200760149\|\|\|AU2008217572; US20080031801; WO200760149\|CN1153482; CN101010129; WO2008101293\|	(EP2393577)\|Search Report references [Examiner]\|-No further relevant documents disclosed\|-See also references of WO 2010088738A1\|\|(WO2010/088738)\|International Search Report [Examiner]\|-See also references of EP 2393577A4\|\|\|\|\|	LAPSED	(EP2393577)\|LAPSED\|(WO2010/088738)\|LAPSED\|(CN102395417)\|LAPSED\|(IN6815/DELNP/2011)\|LAPSED\|(HK1164777)\|LAPSED\|(AU2010210311)\|LAPSED	DEAD	(EP2393577)\|DEAD\|(WO2010/088738)\|DEAD\|(CN102395417)\|DEAD\|(IN6815/DELNP/2011)\|DEAD\|(HK1164777)\|DEAD\|(AU2010210311)\|DEAD	(EP2393577)\|LEGAL DETAILS FOR EP2393577\|Actual or expected expiration date=2014-09-02\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-08\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP10738163\|Application date=2010-02-08\|Standardized application number=2010EP-0738163\|Event publication date=2011-11-11\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2011-12-14\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2393577\|Publication stage code=A1\|Publication date=2011-12-14\|Standardized publication number=EP2393577\|Event publication date=2011-12-14\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2011-09-06\|Event publication date=2011-12-14\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR\|Event publication date=2012-05-16\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2012-08-01\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP2393577\|Publication stage code=A4\|Publication date=2012-08-01\|Standardized publication number=EP2393577\|Event publication date=2012-08-01\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2012-06-29\|Event publication date=2012-08-01\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-08-01\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-08-01\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2015-01-16\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2015-02-18\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2014-09-02\|MEMBER STATE LEGAL DETAILS FOR HK\|Actual or expected expiration date=2018-08-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HK Corresponding appl: HK1164777\|Event publication date=2012-09-28\|Event code=EP/REG\|Event code=HK/DE\|Event group=Examination events\|Reference to a national code\|Requests to designate patent in hong kong\|Requests to record published in hong kong\|Corresponding cc:\|Designated or member state=HK\|Event publication date=2018-08-31\|Event code=EP/REG\|Event code=HK/WD\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Applications withdrawn, deemed to be withdrawn, or refused after publication in hong kong\|Corresponding cc:\|Designated or member state=HK\|(WO2010/088738)\|LEGAL DETAILS FOR WO2010/088738\|Actual or expected expiration date=2012-08-06\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-08\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOAU2010000124\|Application date=2010-02-08\|Standardized application number=2010WO-AU00124\|Event publication date=2010-08-12\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2010088738\|Publication stage code=A1\|Publication date=2010-08-12\|Standardized publication number=WO201088738\|Event publication date=2012-08-06\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2010210311\|Actual or expected expiration date=2014-09-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2010210311\|Application date in the designated or member state=2010-02-08\|Application number in the designated or member state=2010AU-0210311\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2010210311\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2011-09-01\|Publication number in the designated or member state=AU2010210311\|Event publication date=2011-08-15\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2011-09-01\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2014-09-04\|Event code=AU/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=AU\|MEMBER STATE LEGAL DETAILS FOR CN102395417\|Actual or expected expiration date=2014-12-03\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN201080013080\|Application date in the designated or member state=2010-02-08\|Application number in the designated or member state=2010CN-80013080\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN102395417\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-03-28\|Publication number in the designated or member state=CN102395417\|Event publication date=2010-02-08\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CN\|Event publication date=2014-12-03\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2011-08-08\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2011-08-08\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP2393577\|Actual or expected expiration date=2014-09-02\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP10738163\|Application date in the designated or member state=2010-02-08\|Application number in the designated or member state=2010EP-0738163\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2393577\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2011-12-14\|Publication number in the designated or member state=EP2393577\|Event publication date=2010-09-29\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2011-09-06\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2015-02-18\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR HK1164777\|Actual or expected expiration date=2017-09-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HK Corresponding appl: HK12105806\|Application date in the designated or member state=2012-06-14\|Application number in the designated or member state=2012HK-0105806\|Corresponding cc:\|Designated or member state=HK Corresponding pat: HK1164777\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-09-28\|Publication number in the designated or member state=HK1164777\|Event publication date=2012-09-28\|Event code=HK/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=HK\|MEMBER STATE LEGAL DETAILS FOR IN6815/DELNP/2011\|Actual or expected expiration date=2022-12-14\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN6815/DELNP/2011\|Application date in the designated or member state=2011-09-06\|Application number in the designated or member state=2011IN-DN06815\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN6815/DELNP/2011\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-12-14\|Publication number in the designated or member state=IN2011DN06815\|Event publication date=2011-09-06\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|Event publication date=2012-12-14\|Event code=IN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IN\|(CN102395417)\|LEGAL DETAILS FOR CN102395417\|Actual or expected expiration date=2014-12-03\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-08\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201080013080\|Application date=2010-02-08\|Standardized application number=2010CN-80013080\|Event publication date=2012-03-28\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN102395417\|Publication stage code=A\|Publication date=2012-03-28\|Standardized publication number=CN102395417\|Event publication date=2012-03-28\|Event code=CN/C06\|Event indicator=Pos\|Event group=Examination events\|Publication\|Event publication date=2012-05-09\|Event code=CN/C10\|Event group=Examination events\|Request of examination as to substance\|Event publication date=2014-12-03\|Event code=CN/C02\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Deemed withdrawal of patent application after publication (patent law 2001)\|(IN6815/DELNP/2011)\|LEGAL DETAILS FOR IN6815/DELNP/2011\|Actual or expected expiration date=2022-12-14\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-09-06\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN6815/DELNP/2011\|Application date=2011-09-06\|Standardized application number=2011IN-DN06815\|Event publication date=2012-12-14\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN6815/DELNP/2011\|Publication stage code=A\|Publication date=2012-12-14\|Standardized publication number=IN2011DN06815\|Event publication date=2022-12-14\|Event code=IN/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(HK1164777)\|LEGAL DETAILS FOR HK1164777\|Actual or expected expiration date=2017-09-28\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-14\|Event code=HK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=HK HK12105806\|Application date=2012-06-14\|Standardized application number=2012HK-0105806\|Event publication date=2012-09-28\|Event code=HK/A\|Event indicator=Pos\|Event group=Examination events\|Standard patent (R) application\|Publication country=HK\|Publication number=HK1164777\|Publication stage code=A\|Publication date=2012-09-28\|Standardized publication number=HK1164777\|Event publication date=2017-09-28\|Event code=HK/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(AU2010210311)\|LEGAL DETAILS FOR AU2010210311\|Actual or expected expiration date=2014-09-04\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-08\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2010210311\|Application date=2010-02-08\|Standardized application number=2010AU-0210311\|Event publication date=2011-09-01\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2010210311\|Publication stage code=A1\|Publication date=2011-09-01\|Standardized publication number=AU2010210311\|Event publication date=2014-09-04\|Event code=AU/MK4\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application lapsed section 142(2)(d) - no continuation fee paid for the application	(EP2393577)\|Contracting States: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2010/088738)\|ARIPO: GH, GM, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2010/088738)\|EAPO: RU, TJ, BY, MD, AZ, TM, AM, KG, KZ\|(WO2010/088738)\|EPO: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2010/088738)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2010/088738)\|National States: PT, HN, HR, HU, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KM, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PE, PG, PH, PL		https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=NoFk66ibPDQqLsHudby62XmXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO201088738&ekey=1500&xpn=EP2393577&kind=A4	https://register.epo.org/application?number=EP10738163	https://permalink.orbit.com/RenderStaticFirstPage?XPN=DDKAB7Lhfd7dGqGyRhNS9XfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	AU	(WO2010/088738)\|AU	(WO2010/088738)\|NAME=HUNWICK, Richard, J. 59 Abingdon Road, Roseville, New South Wales 2069 , COUNTRY=AU	(EP2393577)\|BE\|(EP2393577)\|BE\|(WO2010/088738)\|AU\|\|(HK1164777)\|HK\|(AU2010210311)\|AU	(EP2393577)\|NAME=De Clercq, Ann G. Y.;De Clercq & Partners Edgard Gevaertdreef 10a , CITY=9830 Sint-Martens-Latem , COUNTRY=BE , REG=101201288\|(EP2393577)\|NAME=De Clercq, Ann G. Y.;De Clercq & Partners Edgard Gevaertdreef 10a , CITY=9830 Sint-Martens-Latem , COUNTRY=BE , REG=101201288\|(WO2010/088738)\|NAME=GRIFFITH HACK Level 29, Northpoint, 100 Miller Street, North Sydney, New South Wales 2060 , COUNTRY=AU\|(CN102395417)\|NAME=LIU JIFU;CHINABLE INTELLECTUAL PROPERTY NAME=WANG LEI;CHINABLE INTELLECTUAL PROPERTY\|(HK1164777)\|NAME=MARKS & CLERK , COUNTRY=HK\|(AU2010210311)\|NAME=Griffith Hack Level 29, Northpoint 100 Miller Street , CITY=North Sydney , STATE=NSW , POSTCODE=2060 , COUNTRY=AU	(EP2393577)\|AU\|(EP2393577)\|AU\|(WO2010/088738)\|AU\|\|(IN6815/DELNP/2011)\|AU\|\|	(EP2393577)\|NAME=Hunwick, Richard J. 59 Abingdon Road, CITY=Roseville NSW 2069, COUNTRY=AU\|(EP2393577)\|NAME=Hunwick, Richard J. 59 Abingdon Road, CITY=Roseville NSW 2069, COUNTRY=AU\|(WO2010/088738)\|NAME=HUNWICK, Richard, J. 59 Abingdon Road, Roseville, New South Wales 2069, COUNTRY=AU\|(CN102395417)\|NAME=HUNWICK RICHARD J\|(IN6815/DELNP/2011)\|NAME=HUNWICK RICHARD J, COUNTRY=AU\|(HK1164777)\|NAME=Hunwick Richard J\|(AU2010210311)\|NAME=Hunwick, Richard J.	(WO2010/088738)\|6\|(IN6815/DELNP/2011)\|6\|(CN102395417)\|6\|(AU2010210311)\|6	3	6			(EP2393577)\|WO2010/088738\|(CN102395417)\|WO2010/088738\|(IN6815/DELNP/2011)\|WO2010/088738\|(HK1164777)\|WO2010/088738\|(AU2010210311)\|WO2010/088738		Primary examiner: Polesak, Helmut\|\|Primary examiner: Polesak, Helmut\|\|(WO2010/088738)\|Number of Claims: NCL=45\|Extended kind: EXTK=x\|\|(CN102395417)\|Number of Claims: NCL=45\|Gazette date: GAZDATE=2012-03-28\|Gazette number: GAZNUM=28-13\|Substantial examination effective date: 20120509\|Number of Pages: NPAGES=26\|\|(IN6815/DELNP/2011)\|Number of Claims: NCL=45\|\|(AU2010210311)\|Number of Claims: NCL=13\|		(EP2393577)\|ENGLISH (ENG)	(IN2011DN06815)\|Patent\|(HK1164777)\|Patent\|(EP2393577)\|Patent\|(CN102395417)\|Patent\|(EP2393577)\|Patent\|(AU2010210311)\|Patent\|(WO201088738)\|Patent	Titre: (EP2393577)\|System, apparatus and method for carbon dioxide sequestration Résumé: (EP2393577)\|A carbon dioxide capture and sequestration process includes a first stage of scrubbing a gas stream containing carbon dioxide with a solution comprising normal ammonium carbonate that is able to absorb the carbon dioxide whereby the carbon dioxide reacts with the ammonium carbonate to produce a solution comprising ammonium bicarbonate. In a second stage, a reactive slurry consisting of a metal silicate rock together with the ammonium bicarbonate solution is passed through a reactor that is controlled so as to promote the reaction between the bicarbonate and the silicate rock to produce metal carbonate and silica.	2	Abstract	gpt-4o-mini	yes	The patent describes a process that involves the reaction of ammonium bicarbonate with metal silicate rocks to produce metal carbonates, which aligns with the topic of enhanced weathering and CO₂ sequestration.
6	CN202411977823	CN202411977823	CN119607861	113778323	CN119607861 A 2025-03-14 [CN119607861]	2024-12-31	2024-12-31	2025-03-14		(CN119607861)\|2044-12-31	(CN119607861)\|Carbon capture and storage system and carbon capture and storage method	(CN119607861)\|The invention relates to the technical field of flue gas treatment, in particular to a carbon capture and storage system and a carbon capture and storage method.The carbon capture and storage system comprises a waste gas absorption unit, an amine liquid circulation unit, a carbon dioxide gas salinization unit and a carbon sequestration unit which are communicated in sequence; the system further comprises a limestone slurry pulping and filling unit; and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. The carbon capture and storage method is a brand-new organic amine decarburization and permanent carbon sequestration method provided on the basis of the principle of enhancing rock weathering; compared with a traditional carbon sequestration method that carbon dioxide is transported through compression and liquefaction and stored in an underground salt water layer, the method has the advantages that the carbon capturing and storing process is short, high-pressure and low-temperature high-energy-consumption equipment does not need to be used, the captured carbon dioxide gas does not need to be stored and transported at low temperature, energy consumption can be reduced, the carbon sequestration cost is saved, and the carbon sequestration efficiency is improved. The carbon dioxide escape phenomenon in the storage and transportation process can be avoided, and the carbon sequestration efficiency is improved.	SINOTECH ENERGY\|ZHONGTAI CARBON SHANGHAI ENVIRONMENTAL PROTECTION SCIENCE & TECHNOLOGY	(CN119607861)\|SINOTECH ENERGY CO., LTD. ([CN])\|ZHONGTAI CARBON SHANGHAI ENVIRONMENTAL PROTECTION SCIENCE AND TECH LIMITED COMPANY	WEI YING\|HE WEI	(CN119607861)\|WEI YING\|HE WEI		(CN119607861)\|Compared with the prior art, the invention has the advantages that: (1) The invention provides a carbon capture storage system and a carbon capture storage method, wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine, then resolving the carbon dioxide gas in a desorption tower, then reacting the resolved carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, and finally sealing the calcium bicarbonate in a deep sea discharge area; compared with the traditional carbon fixation method of carbon dioxide through compression, liquefaction and transportation and underground salty water layer sealing, the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short, high-pressure and low-temperature high-energy equipment is not needed in the carbon capture and sealing process, the low-temperature storage and transportation of captured carbon dioxide gas are not needed, the energy consumption can be reduced, the carbon fixation cost can be saved, the phenomenon of carbon dioxide escape in the storage and transportation process can be avoided, the carbon fixation efficiency is improved, meanwhile, the consumption in the aspects of manpower and material resources can be reduced, and the problems of overlong carbon capture and sealing flow, high energy consumption, high cost, high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved.\|	(CN119607861)\|1. The carbon capturing and storing system is characterized by comprising an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit, a carbon fixation and sealing unit and a limestone slurry pulping and filling unit; The waste gas absorption unit comprises a temperature reduction tower and an absorption tower, wherein the upper part of the temperature reduction tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reduction tower is communicated with the absorption tower, a seawater spraying device is arranged in the temperature reduction tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reduction tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through a water conveying pipeline, the bottom of the temperature reduction tower is also provided with a seawater outlet, the upper end in the absorption tower is provided with a lean amine liquid spraying device, and the top of the absorption tower is provided with an exhaust port; The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. \|	(CN119607861)\|The invention provides a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.Disclosure of InventionThe invention aims to provide a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|The invention relates to the technical field of flue gas treatment, in particular to a carbon capture storage system and a carbon capture storage method.\|The invention relates to the technical field of flue gas treatment, in particular to a carbon capturing and storing system and a carbon capturing and storing method, comprising an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salifying unit and a carbon fixing and sealing unit which are sequentially communicated; the device also comprises a limestone slurry pulping and filling unit which is communicated with the carbon dioxide gas salinization unit.\|	(CN119607861)\|DESORPTION TOWER(100,39)\|CARBON CAPTURE(100,17)\|CARBON(100,15)\|CARBON CAPTURE STORAGE(100,13)\|STORAGE SYSTEM(100,13)\|CARBON CAPTURE STORAGE SYSTEM(100,11)\|LIMESTONE SLURRY POND(87,21)\|CARBONIZATION TANK(85,38)\|ABSORPTION TOWER(84,60)\|LIMESTONE SLURRY(74,32)\|SLAG DISCHARGE(72,6)\|AMINE DECARBURIZATION STORAGE(62,4)\|REGENERATING GAS COOLER(57,14)\|ORGANIC AMINE DECARBURIZATION STORAGE(54,4)\|CONVEYING PIPELINE(51,9)\|DECARBURIZATION STORAGE(51,4)\|SLURRY POND(49,21)\|SEAWATER PUMP(49,9)\|GAS SALINIZATION(48,8)\|FLUE GAS CONVEYING PIPELINE(44,9)\|ORGANIC AMINE DECARBURIZATION(44,1)\|LEAN AMINE LIQUID(42,27)\|AMINE DECARBURIZATION(42,1)\|CARBONIZATION TANK BOTTOM(38,12)\|AMINE LIQUID(37,54)\|COMPRESSOR(35,26)\|CARBON DIOXIDE GAS SALINIZATION(35,8)\|CONVEYING LIMESTONE SLURRY RESIDUE(34,2)\|BUBBLE DISTRIBUTOR(33,8)\|LEAN LIQUID COOLER(32,6)\|SEAWATER(31,27)\|COOLED LEAN AMINE(31,4)\|LEAN RICH LIQUID INLET(30,2)\|GAS SALIFYING(29,2)\|MANPOWER(29,2)\|WATER CONVEYING PIPELINE(29,2)\|ENHANCED ROCK(29,1)\|RICH AMINE LIQUID(28,19)\|CONVEYING LIMESTONE POWDER(28,2)\|OVERLONG CARBON CAPTURE(28,1)\|CARBON DIOXIDE(27,65)\|TEMPERATURE REDUCTION TOWER(27,29)\|AMINE LIQUID CIRCULATION(27,6)\|LIMESTONE SLURRY TANK(27,4)\|SEAWATER OUTLET(26,5)\|CARBON DIOXIDE GAS(25,33)\|LIQUID CLARIFICATION(25,12)\|REBOILER(25,10)\|LEAN LIQUID INLET(25,6)\|RICH LIQUID HEAT EXCHANGER(25,6)\|TREATING FLUE GAS(25,2)\|LEAN LIQUID PUMP(24,9)\|TRANSPORTATION(24,8)\|LIQUEFACTION(24,3)\|CARBON DIOXIDE ESCAPE(24,2)\|CARBON FIXATION(23,11)\|SOLUBLE CALCIUM BICARBONATE(23,7)\|CARBON DIOXIDE GAS SALIFYING(23,2)\|FLUE GAS(22,22)\|LIQUID CIRCULATION(22,6)\|FIXED CARBON FIXATION(22,1)\|LEAN RICH SOLUTION(22,1)\|RICH LIQUID PUMP(21,11)\|RICH LIQUID INLET(21,6)\|LEAN LIQUID OUTLET(21,3)\|ROCK REINFORCEMENT(21,3)\|LARGE MANPOWER(21,2)\|GAS OUTLET(20,10)\|CARBON FIXING(20,6)\|CALCIUM BICARBONATE(19,14)\|MIXER(19,12)\|LIMESTONE(19,7)\|BOOSTER FAN(19,3)\|RICH LIQUID OUTLET(19,3)\|DECARBURIZATION TREATMENT(19,2)\|LEAN SOLUTION COOLER(19,2)\|CONSUMPTION EQUIPMENT(19,1)\|ACIDIC CONDITION(18,6)\|SLAG DISCHARGE PUMP(18,4)\|EQUIPMENT RESOURCE CONSUMPTION(18,3)\|LEAN(18,2)\|DEEP SEA DISCHARGE AREA(17,8)\|SALTY WATER LAYER SEALING(17,2)\|SEALING FLOW(17,2)\|WATER FLOW PIPELINE(16,6)\|HEAT EXCHANGER(15,26)\|LIMESTONE SLURRY PUMP(15,6)\|ORGANIC AMINE(15,4)\|TRANSPORTATION(15,3)\|STEAM ABSORPTION HEAT(14,3)\|CARBON FIXATION COST(14,1)\|BYPASS VALVE(13,8)\|DISCHARGE AREA(13,8)\|SUPERFINE LIMESTONE POWDER(13,3)\|FLUE GAS SOURCE(12,6)\|EXHAUST GAS(12,5)\|CARBONIZATION TANK TOP(12,3)\|DISCHARGE OUTLET(12,3)\|CARBON CAPTURE SEALING(12,2)\|EQUIPMENT RESOURCE(12,1)\|WATER OUTLET(11,6)\|BIN(11,4)\|ENERGY CONSUMPTION(11,3)\|LIQUID HEAT EXCHANGER(11,2)\|WASTE GAS(10,25)\|TEMPERATURE REDUCTION TOWER BOTTOM(10,7)\|EXHAUST PORT(10,4)\|AIRFLOW PIPELINE(10,3)\|CARBON DIOXIDE CARBON FIXING(10,1)\|CARBON FIXING COST(10,1)\|STIRRER(9,7)\|HIGH ENERGY CONSUMPTION(9,3)\|SLURRY CONVEYING PIPELINE(9,2)\|CONVEYING LIMESTONE SLURRY SLAG(9,1)\|SEALING(9,1)\|GENERATED CALCIUM BICARBONATE(8,3)\|COMPRESSOR BOOSTER REFRIGERATOR(8,1)\|MIXED LIQUID(7,6)\|AIR FLOW PIPELINE(7,3)\|DESLAGGING PUMP(7,3)\|PH VALUE(7,2)\|WASTE GAS ABSORPTION UNIT(7,2)\|LIMESTONE POWDER WAREHOUSE(7,1)\|ABSORPTION UNIT(6,2)\|LIMESTONE SEDIMENT(6,1)\|TRIETHYLENE TETRAMINE(6,1)\|MIXER UPPER END(5,3)\|SEAWATER SPRAY(5,1)\|FORMED RICH AMINE LIQUID(4,3)\|BICARBONATE ION(4,2)\|FORMED LEAN AMINE SOLUTION(4,2)\|INPUT END(4,2)\|LEAN AMINE LIQUID SPRAY(4,1)\|SIMULTANEOUSLY CONVEYING LIMESTONE POWDER(4,1)\|AIR OUTLET(3,5)\|CLEAN GAS(3,2)\|DECARBONIZATION(3,2)\|OUTPUT END(3,2)\|ABSORPTION CARBON(3,1)\|CARBON DIOXIDE ESCAPING PHENOMENON(3,1)\|	(CN119607861)\|1. The carbon capturing and storing system is characterized by comprising an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit, a carbon fixation and sealing unit and a limestone slurry pulping and filling unit;\| The waste gas absorption unit comprises a temperature reduction tower and an absorption tower, wherein the upper part of the temperature reduction tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reduction tower is communicated with the absorption tower, a seawater spraying device is arranged in the temperature reduction tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reduction tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through a water conveying pipeline, the bottom of the temperature reduction tower is also provided with a seawater outlet, the upper end in the absorption tower is provided with a lean amine liquid spraying device, and the top of the absorption tower is provided with an exhaust port; \| The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; \| The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; \| The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; \| The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. \|2. The carbon capture and storage system of claim 1, wherein the bottom of the temperature reduction tower is communicated with the bottom of the absorption tower through an air flow pipeline, and a booster fan is arranged on the air flow pipeline between the temperature reduction tower and the absorption tower.\|3. The carbon capture storage system of claim 2, wherein the amine liquid circulation unit further comprises a rich liquid pump and a lean liquid pump, wherein an input end of the rich liquid pump is communicated with the bottom of the absorption tower, an output end of the rich liquid pump is communicated with a rich liquid inlet of the lean-rich liquid heat exchanger, an input end of the lean liquid pump is communicated with the bottom of the desorption tower, and an output end of the lean liquid pump is communicated with a lean liquid inlet of the lean-rich liquid heat exchanger.\|4. A carbon capture storage system according to claim 2, wherein a pressure relief valve is disposed in the gas flow line between the gas outlet and the compressor.\|5. The carbon capture and storage system according to claim 2, wherein a bubble distributor and a stirrer are arranged in the carbonization tank, and the bubble distributor is communicated with the output end of the compressor.\|6. A carbon capture storage system according to claim 2 wherein the bottom of the filter is in communication with a limestone slurry pond, the upper end of the filter is further provided with a gas outlet, and the gas outlet is in communication with the input of the compressor via a gas flow line.\|7. A carbon capture storage method, characterized in that the carbon capture storage system according to any one of claims 1 to 6 is used for carbon capture storage, comprising the steps of:\| S1, when waste gas needs decarburization treatment, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, the temperature is reduced to 40-60 ℃, the waste gas flows into the absorption tower from the bottom of the absorption tower, contacts with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, so that rich amine liquid and relatively pure gas are formed, and the relatively pure gas flows out from a gas outlet; \| S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid from the top of the desorption tower to the bottom of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a reboiler, desorbing carbon dioxide gas and forming lean amine liquid; \| S3, forming lean amine liquid, cooling the lean amine liquid twice through a lean-rich liquid heat exchanger and a lean liquid cooler, conveying the lean amine liquid to the top in an absorption tower, simultaneously, cooling the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing the cooled lean amine liquid to 4-6bar through a compressor, conveying the cooled lean amine liquid to the bottom of a carbonization tank, then, reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition based on a reinforced rock weathering principle to generate soluble calcium bicarbonate, conveying part of unreacted carbon dioxide gas to the compressor from an air outlet at the top of the carbonization tank, and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again; \| S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter for filtering to form clarified liquid and limestone slurry slag, conveying limestone powder and seawater into a limestone slurry tank to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank; \| s5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater in proportion to form mixed liquid with a pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, and conveying limestone slurry residues in the filter into a limestone slurry tank for preparing limestone slurry. \|8. The carbon capture storage method of claim 7, wherein in S2, the twice cooling of the formed lean amine solution comprises cooling to 60-70 ℃ by a lean rich solution heat exchanger and cooling to 30-45 ℃ by a lean solution cooler.\|9. The carbon capture storage method of claim 7, wherein in S5 the ratio of clarified liquid to seawater is 1 (10-1000).	(CN119607861)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of flue gas treatment, in particular to a carbon capture storage system and a carbon capture storage method.\|BACKGROUND ART\|[0002] The carbon dioxide discharged by the large amount of fossil fuels is a main cause of global warming, the carbon dioxide discharged is captured, utilized and sealed, and is one of the most effective means for realizing large-scale carbon emission reduction and coping with climate change, and at present, the carbon dioxide is captured by adopting a chemical absorption carbon capturing technology after the fossil fuels are combusted.\|[0003] The method for decarbonizing and storing the organic amine is one of the most main carbon trapping technologies by a chemical absorption method, and the existing method for decarbonizing and storing the organic amine is a method for capturing and storing the carbon dioxide from the waste gas by utilizing the principle that an organic amine is in contact with the carbon-containing waste gas and is subjected to absorption reaction and then rich liquid is heated and reversibly desorbed, then the carbon dioxide is stored in a liquid tank by utilizing a method of cooling and liquefying a compressor booster refrigerator, and the liquid carbon dioxide is conveyed to underground capable of being permanently stored by transportation, so that the purpose of capturing and storing the carbon dioxide is achieved.\|[0004] In the process of capturing and sealing carbon dioxide by adopting the organic amine decarburization storage method, a large amount of energy is consumed in the processes of compressing, liquefying, storing, transporting, sealing and the like of the carbon dioxide, at least 300KWh of energy is consumed per ton of compressed, liquefied and stored carbon dioxide, and in addition, the carbon dioxide is sealed in a low-temperature, high-pressure storage and high-pressure saline water layer sealing mode, so that the capturing and sealing process of the method is longer, the carbon dioxide is required to be ensured to be in a liquid state during the capturing and sealing process, and high energy is required to be consumed for keeping the liquid state of the carbon dioxide.\|[0005] The invention provides a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|DISCLOSURE\|Disclosure of Invention\|[0006] The invention aims to provide a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|[0007] The technical scheme includes that the carbon capturing and storing system comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salifying unit, a carbon fixing and sealing unit and a limestone slurry pulping and filling unit, wherein the exhaust gas absorbing unit comprises a temperature reducing tower and an absorbing tower, the upper part of the temperature reducing tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reducing tower is communicated with the absorbing tower, a seawater spraying device is arranged in the temperature reducing tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reducing tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through the water conveying pipeline, the bottom of the temperature reducing tower is also provided with a seawater outlet, the upper end of the inside of the absorbing tower is provided with a lean amine liquid spraying device, and the top of the absorbing tower is provided with an exhaust port;\| The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; \| The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; \| The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; \| The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. \|[0008] Preferably, the bottom of the temperature reduction tower is communicated with the bottom of the absorption tower through an airflow pipeline, and a booster fan is arranged on the airflow pipeline between the temperature reduction tower and the absorption tower.\|[0009] Preferably, the amine liquid circulation unit further comprises a rich liquid pump and a lean liquid pump, wherein the input end of the rich liquid pump is communicated with the bottom of the absorption tower, the output end of the rich liquid pump is communicated with a rich liquid inlet of the lean-rich liquid heat exchanger, the input end of the lean liquid pump is communicated with the bottom of the desorption tower, and the output end of the lean liquid pump is communicated with a lean liquid inlet of the lean-rich liquid heat exchanger.\|[0010] Preferably, a pressure reducing valve is arranged on the air flow pipeline between the air outlet and the compressor.\|[0011] Preferably, a bubble distributor and a stirrer are arranged in the carbonization tank, and the bubble distributor is communicated with the output end of the compressor.\|[0012] Preferably, the bottom of the filter is communicated with the limestone slurry pond, the upper end of the filter is also provided with a gas outlet, and the gas outlet is communicated with the input end of the compressor through a gas flow pipeline.\|[0013] The invention also provides a method for capturing and storing carbon by adopting the carbon capturing and storing system, which specifically comprises the following steps:\| S1, when waste gas needs decarburization treatment, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, the temperature is reduced to 40-60 ℃, the waste gas flows into the absorption tower from the bottom of the absorption tower, contacts with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, so that rich amine liquid and relatively pure gas are formed, and the relatively pure gas flows out from a gas outlet; \| S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid from the top of the desorption tower to the bottom of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a reboiler, desorbing carbon dioxide gas and forming lean amine liquid; \| S3, forming lean amine liquid, cooling the lean amine liquid twice through a lean-rich liquid heat exchanger and a lean liquid cooler, conveying the lean amine liquid to the top in an absorption tower, simultaneously, cooling the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing the cooled lean amine liquid to 4-6bar through a compressor, conveying the cooled lean amine liquid to the bottom of a carbonization tank, then, reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition based on a reinforced rock weathering principle to generate soluble calcium bicarbonate, conveying part of unreacted carbon dioxide gas to the compressor from an air outlet at the top of the carbonization tank, and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again; \| S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter for filtering to form clarified liquid and limestone slurry slag, conveying limestone powder and seawater into a limestone slurry tank to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank; \| s5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater in proportion to form mixed liquid with a pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, and conveying limestone slurry residues in the filter into a limestone slurry tank for preparing limestone slurry. \|[0014] Preferably, in S2, the two cooling steps of the formed lean amine solution include cooling to 60-70 ℃ by a lean-rich solution heat exchanger and cooling to 30-45 ℃ by a lean solution cooler.\|[0015] Preferably, in S5, the ratio of clarified liquid to seawater is 1 (10-1000).\|[0016] Compared with the prior art, the invention has the advantages that:\| (1) The invention provides a carbon capture storage system and a carbon capture storage method, wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine, then resolving the carbon dioxide gas in a desorption tower, then reacting the resolved carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, and finally sealing the calcium bicarbonate in a deep sea discharge area; compared with the traditional carbon fixation method of carbon dioxide through compression, liquefaction and transportation and underground salty water layer sealing, the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short, high-pressure and low-temperature high-energy equipment is not needed in the carbon capture and sealing process, the low-temperature storage and transportation of captured carbon dioxide gas are not needed, the energy consumption can be reduced, the carbon fixation cost can be saved, the phenomenon of carbon dioxide escape in the storage and transportation process can be avoided, the carbon fixation efficiency is improved, meanwhile, the consumption in the aspects of manpower and material resources can be reduced, and the problems of overlong carbon capture and sealing flow, high energy consumption, high cost, high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved. \|[0017] (2) The carbon capture storage system and the carbon capture storage method provided by the invention are characterized in that the carbon capture storage method is used for converting the resolved carbon dioxide gas and limestone slurry into calcium bicarbonate under an acidic condition, and the calcium bicarbonate can exist stably in the form of bicarbonate ions and calcium ions under deep sea and low temperature conditions, so that the carbon capture storage method can realize the purpose of permanently fixing carbon.\|DRAWINGS DESCRIPTION\|[0018] The invention is further described below with reference to the accompanying drawings and examples:\| FIG. 1 is a schematic diagram of a carbon capture storage system according to the present invention; \| The device comprises a temperature reduction tower, a2 absorption tower, a3 bypass valve, a 4 sea water pump, a 5 sea water outlet, a 6, an exhaust port, a7, a desorption tower, a 8, a lean-rich liquid heat exchanger, a9, a reboiler, a 10, a lean liquid cooler, a 11, a regenerated gas cooler, a 12, a compressor, a 13, a carbonization tank, a 14, an air outlet, a 15, a slag discharge pump, a 16, a filter, a 17, a mixer, a 18, a water outlet, a 19, a PH meter, a 20, a limestone slurry pond, a 21, a limestone powder warehouse, a 22, a booster fan, a 23, a rich liquid pump, a 24, a lean liquid pump, a 25, a pressure reducing valve, a 26, a bubble distributor, a 27, a stirrer, a 28, a gas outlet, a 29 and a limestone slurry pump. \|INVENTION MODE\|Detailed Description\|[0019] The following describes the present invention in further detail with reference to specific examples:\| A carbon capturing and storing system is shown in fig. 1, and comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit and a carbon fixation and sealing unit which are sequentially communicated, wherein the carbon capturing and storing system also comprises a limestone slurry pulping and filling unit, and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. \|[0020] The waste gas absorption unit comprises a temperature reduction tower 1 and an absorption tower 2; the upper part of the temperature reduction tower 1 is communicated with a flue gas source through a flue gas conveying pipeline, and a bypass valve 3 is arranged on the flue gas conveying pipeline between the temperature reduction tower 1 and the flue gas source; the bypass valve 3 is opened to convey the waste gas to be decarbonized into the temperature reduction tower 1 for cooling treatment, a seawater spray device is arranged at the upper end of the interior of the temperature reduction tower 1, the seawater spray device is connected with the output end of a seawater pump 4 positioned outside the temperature reduction tower 1 through a water pipeline, the seawater is conveyed into the temperature reduction tower 1, the upper end of the temperature reduction tower 1 sprays the waste gas to the bottom of the temperature reduction tower 1 and fully contacts and mixes the waste gas conveyed into the temperature reduction tower 1 to further reduce the temperature of the waste gas, the bottom of the temperature reduction tower 1 is communicated with the absorption tower 2 and is used for conveying the waste gas subjected to the spray cooling treatment into the absorption tower 2, a seawater outlet 5 is also arranged at the bottom of the temperature reduction tower 1, a water pipeline leading to a seawater discharge area is connected at the seawater outlet 5 and is used for discharging the seawater sprayed to the bottom of the temperature reduction tower 1 into the sea, a lean amine liquid spray device is arranged at the upper end of the absorption tower 2 and is used for spraying the lean amine liquid from the upper end of the absorption tower 2 to a filler position close to the bottom of the absorption tower 2 and is fully contacted with the waste gas conveyed into the absorption tower 2, the waste gas is further reduced in temperature, the bottom of the absorption tower 2 is in contact with the waste gas is formed by the pure amine gas and the pure amine gas is discharged into the absorption tower 2 through the clean gas after the absorption tower 2 is relatively connected to the top of the absorption tower 2 through the clean gas which is relatively arranged to the top of the absorption tower 2, and the booster fan 22 is further arranged on the airflow pipeline between the temperature reduction tower 1 and the absorption tower 2 and is used for increasing the pressure of the waste gas conveyed into the absorption tower 2, increasing the flow speed and the airflow energy of the waste gas, and fully mixing the waste gas with the lean amine liquid in the absorption tower 2, so that the carbon dioxide gas in the waste gas fully contacts with the lean amine liquid and is absorbed by the lean amine liquid, and capturing the carbon dioxide gas in the waste gas is realized.\|[0021] The amine liquid circulation unit comprises a desorption tower 7, a lean-rich liquid heat exchanger 8 and a reboiler 9, wherein the reboiler 9 is communicated with the desorption tower 7 and is connected to a position close to the bottom of the desorption tower 7, namely a filler, a rich liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the absorption tower 2, a rich liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the desorption tower 7 and is used for heating the rich amine liquid at the bottom of the absorption tower 2 and then conveying the rich amine liquid to the top of the desorption tower 7, a spraying device at the top of the desorption tower 7 is used for spraying the rich amine liquid close to the bottom of the desorption tower 7 from the top of the desorption tower 7, the rich amine liquid sprayed to the filler absorbs steam heat generated by the reboiler 9 and then heats and desorbs carbon dioxide to form lean amine liquid containing only a small amount of carbon dioxide, and flows to the bottom of the desorption tower 7, a lean liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the desorption tower 7, a lean liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the absorption tower 2 through a lean liquid cooler 10 and is used for cooling the lean liquid at the bottom of the absorption tower 2, and is conveyed to the top of the absorption tower 2 from the lean liquid heat exchanger 8 to the top of the absorption tower 2 through the lean liquid heat exchanger 10 and then is recycled to the absorption tower 2. In order to ensure continuous and stable mutual circulation and transportation of the rich amine liquid and the lean amine liquid formed in the absorption tower 2 and the desorption tower 7 so as to achieve the effect of recycling the organic amine liquid, the amine liquid circulation unit further comprises a rich liquid pump 23 and a lean liquid pump 24, wherein the input end of the rich liquid pump 23 is communicated with the bottom of the absorption tower 2, the output end of the rich liquid pump is communicated with the rich liquid inlet of the lean-rich liquid heat exchanger 8 and is used for pumping the rich amine liquid formed in the absorption tower 2 into the lean-rich liquid heat exchanger 8 and transporting the rich amine liquid into the desorption tower 7, and similarly, the input end of the lean liquid pump 24 is communicated with the bottom of the desorption tower 7, and the output end of the rich liquid pump 24 is communicated with the lean liquid inlet of the lean-rich liquid heat exchanger 8.\|[0022] The carbon dioxide gas salinization unit comprises a regeneration gas cooler 11, a compressor 12 and a carbonization tank 13, wherein the input end of the regeneration gas cooler 11 is communicated with the top of the desorption tower 7, the output end of the regeneration gas cooler is communicated with the input end of the compressor 12, the output end of the compressor 12 is communicated with the bottom of the carbonization tank 13, carbon dioxide gas desorbed in the desorption tower 7 is cooled by the regeneration gas cooler 11, dehydrated and then flows into the compressor 12, the compressor 12 is pressurized and then is conveyed into the carbonization tank 13, and based on the rock weathering principle, the carbon dioxide gas and limestone slurry in the carbonization tank 13 are mixed and react under the acidic condition to form soluble calcium bicarbonate. In order to sufficiently mix and sufficiently react the carbon dioxide gas with the limestone slurry in the carbonization tank 13, a bubble distributor 26 and a stirrer 27 may be provided in the carbonization tank 13, the bubble distributor 26 may be connected to the output end of the compressor 12, the carbon dioxide gas supplied into the carbonization tank 13 by the compressor 12 may be separated into fine bubbles by the bubble distributor 26, the dissolution efficiency of the carbon dioxide gas in the limestone slurry may be improved, the contact ratio of the carbon dioxide gas with the limestone slurry may be increased, and the reaction efficiency may be improved, and the carbon dioxide gas and the limestone slurry in the carbonization tank 13 may be sufficiently mixed and reacted with each other by stirring by the stirrer 27, thereby further improving the conversion rate of the carbon dioxide.\|[0023] The carbon sequestration unit comprises a deslagging pump 15, a filter 16 and a mixer 17, wherein the input end of the deslagging pump 15 is communicated with the bottom of the carbonization tank 13, the output end of the deslagging pump 15 is communicated with the filter 16 and is used for conveying soluble calcium bicarbonate and limestone slurry generated by the reaction at the bottom of the carbonization tank 13 into the filter 16 together for filtering, the upper end of the filter 16 is communicated with the mixer 17, the upper end of the mixer 17 is communicated with the output end of the sea water pump 4 through a water flow pipeline, the lower end of the mixer 17 is provided with a water outlet 18, the water outlet 18 is communicated with a water flow pipeline leading to a deep sea discharge area, the clarified liquid separated from the filter 16 is conveyed into the mixer 17 and is mixed with sea water from the sea water pump 4 in the mixer 17 to form mixed liquid, then the mixed liquid is discharged into the deep sea discharge area through the water flow pipeline to achieve the purpose of permanently sequestration, and a PH meter 19 is further arranged at the water outlet 18 and is used for monitoring the PH value of the mixed liquid and the sea water, and the clear liquid is discharged into the deep sea after the PH value of the clear liquid meets the requirements. The upper end of the filter 16 is also provided with a gas outlet 28, and the gas outlet 28 is communicated with the input end of the compressor 12 through a gas flow pipeline and is used for conveying the carbon dioxide gas which is conveyed into the filter 16 together with the soluble calcium bicarbonate and limestone slurry into a carbon dioxide gas salinization unit for continuous salinization.\|[0024] The limestone slurry pulping and filling unit comprises a limestone slurry pond 20, wherein the upper part of the limestone slurry pond 20 is respectively communicated with a limestone powder bin 21 and the output end of a sea water pump 4, and is used for adding superfine limestone powder and sea water in the limestone powder bin 21 into the limestone slurry pond 20 together and uniformly mixing the superfine limestone powder and the sea water in the limestone slurry pond 20 to form limestone slurry, a stirrer 27 is further arranged in the limestone slurry pond 20, stirring is performed by adopting the stirrer 27 in the process of adding the limestone powder and the sea water into the limestone slurry pond 20, so that rapid uniform mixing of the limestone powder and the sea water is facilitated, the bottom of the limestone slurry pond 20 is communicated with the upper part of a carbonization tank 13 through a slurry conveying pipeline, a limestone slurry pump 29 is arranged on the slurry conveying pipeline, and the limestone slurry in the limestone slurry pond 20 is pumped into the carbonization tank 13 through the limestone slurry pump 29 to perform internal reaction. The bottom of the filter 16 is also communicated with the limestone slurry pond 20, and limestone sediment formed at the lower layer in the filter 16 is conveyed into the limestone slurry pond 20 and is used as a raw material together with superfine limestone powder to prepare limestone slurry.\|[0025] The method for capturing and storing carbon by adopting the carbon capturing and storing system specifically comprises the following steps:\| S1, when the waste gas needs to be decarbonized, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, seawater sprayed through a Wen Dana is fully contacted with the flue gas and absorbs heat brought by the flue gas, so that the flue gas is cooled to be within a range of 40-60 ℃, then, the waste gas flows into the absorption tower from the bottom of the absorption tower, is contacted with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, rich amine liquid and relatively pure gas are formed, and the relatively pure gas is discharged into the atmosphere from an exhaust port at the top of the absorption tower or is conveyed to a subsequent gas treatment unit. Wherein, the flue gas is conveyed into a temperature reduction tower according to the gas flow of 50-500L/h, the lean amine liquid in the absorption tower can be one of aqueous solution or mixed aqueous solution of a plurality of methyl diethanolamine, ethanolamine, triethylene tetramine and the like, and the concentration of carbon dioxide gas in the relatively pure gas is below 2.0 percent (mole percent). \|[0026] S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid to the bottom from the top of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a bottom reboiler, desorbing carbon dioxide gas, forming lean amine liquid, and flowing to the bottom of the desorption tower.\|[0027] S3, cooling the lean amine liquid at the bottom of the desorption tower to 60-70 ℃ through a lean-rich liquid heat exchanger, cooling to 30-45 ℃ through a lean liquid cooler, conveying the lean amine liquid to the top of the absorption tower, spraying the lean amine liquid to the bottom of the absorption tower from the top in the absorption tower, simultaneously, cooling and dewatering the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing to 4-6bar through a compressor, and conveying the carbon dioxide gas to the bottom of a carbonization tank, and then, based on the reinforced rock weathering principle, absorbing and reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, wherein the reaction equation is as follows: And conveying part of unreacted carbon dioxide gas to a compressor from an air outlet at the top of the carbonization tank, compressing and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again. \|[0028] S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter according to the flow ratio of 5-100L/h for filtering to form clarified liquid and limestone slurry slag, simultaneously conveying limestone powder and seawater into a limestone slurry pond to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank according to the flow ratio of 5-100L/h.\|[0029] S5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater according to the proportion of 1 (10-1000), forming mixed liquid with the pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, achieving the purpose of carbon fixation and sealing, and conveying limestone slurry slag in the filter into a limestone slurry pond for preparing limestone slurry.\|[0030] Compared with the traditional carbon fixation method for sealing and storing carbon dioxide through compression, liquefaction and transportation and an underground salty water layer, the carbon capture and storage method does not need high-pressure and low-temperature high-energy equipment, low-temperature storage and transportation, saves the cost consumed in the low-temperature storage, transportation and sealing and storage processes, avoids the carbon dioxide escaping phenomenon in the transportation process, greatly shortens the carbon fixation process, and reduces the carbon fixation energy consumption. In addition, because the calcium bicarbonate exists in the form of bicarbonate ions and calcium ions in the sea water and can exist stably under deep sea and low temperature conditions, the carbon capturing and storing method can better achieve the purpose of carbon fixation and sealing.\|[0031] The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and implement the same according to the content of the present invention, and are not intended to limit the scope of the present invention. It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof, and it is therefore desired that the present invention be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.	(CN119607861)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of flue gas treatment, in particular to a carbon capture storage system and a carbon capture storage method.\|BACKGROUND ART\|[0002] The carbon dioxide discharged by the large amount of fossil fuels is a main cause of global warming, the carbon dioxide discharged is captured, utilized and sealed, and is one of the most effective means for realizing large-scale carbon emission reduction and coping with climate change, and at present, the carbon dioxide is captured by adopting a chemical absorption carbon capturing technology after the fossil fuels are combusted.\|[0003] The method for decarbonizing and storing the organic amine is one of the most main carbon trapping technologies by a chemical absorption method, and the existing method for decarbonizing and storing the organic amine is a method for capturing and storing the carbon dioxide from the waste gas by utilizing the principle that an organic amine is in contact with the carbon-containing waste gas and is subjected to absorption reaction and then rich liquid is heated and reversibly desorbed, then the carbon dioxide is stored in a liquid tank by utilizing a method of cooling and liquefying a compressor booster refrigerator, and the liquid carbon dioxide is conveyed to underground capable of being permanently stored by transportation, so that the purpose of capturing and storing the carbon dioxide is achieved.\|[0004] In the process of capturing and sealing carbon dioxide by adopting the organic amine decarburization storage method, a large amount of energy is consumed in the processes of compressing, liquefying, storing, transporting, sealing and the like of the carbon dioxide, at least 300KWh of energy is consumed per ton of compressed, liquefied and stored carbon dioxide, and in addition, the carbon dioxide is sealed in a low-temperature, high-pressure storage and high-pressure saline water layer sealing mode, so that the capturing and sealing process of the method is longer, the carbon dioxide is required to be ensured to be in a liquid state during the capturing and sealing process, and high energy is required to be consumed for keeping the liquid state of the carbon dioxide.\|[0005] The invention provides a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|DISCLOSURE\|Disclosure of Invention\|[0006] The invention aims to provide a carbon capture storage system and a carbon capture storage method, which are used for solving the problems of overlong carbon capture sealing process, high energy consumption, high cost, large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art.\|[0007] The technical scheme includes that the carbon capturing and storing system comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salifying unit, a carbon fixing and sealing unit and a limestone slurry pulping and filling unit, wherein the exhaust gas absorbing unit comprises a temperature reducing tower and an absorbing tower, the upper part of the temperature reducing tower is communicated with a flue gas source through a flue gas conveying pipeline, the bottom of the temperature reducing tower is communicated with the absorbing tower, a seawater spraying device is arranged in the temperature reducing tower, a bypass valve is arranged on the flue gas conveying pipeline between the temperature reducing tower and the flue gas source, the seawater spraying device is connected with the output end of a seawater pump through the water conveying pipeline, the bottom of the temperature reducing tower is also provided with a seawater outlet, the upper end of the inside of the absorbing tower is provided with a lean amine liquid spraying device, and the top of the absorbing tower is provided with an exhaust port;\| The amine liquid circulation unit comprises a desorption tower, a lean and rich liquid heat exchanger and a reboiler, wherein the reboiler is communicated with the desorption tower, a rich liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the absorption tower, a rich liquid outlet is communicated with the top of the desorption tower, a lean liquid inlet of the lean and rich liquid heat exchanger is communicated with the bottom of the desorption tower, and a lean liquid outlet is communicated with the top of the absorption tower after passing through a lean liquid cooler; \| The carbon dioxide gas salinization unit comprises a regeneration gas cooler, a compressor and a carbonization tank, wherein the input end of the regeneration gas cooler is communicated with the top of the desorption tower, the output end of the regeneration gas cooler is communicated with the input end of the compressor, and the output end of the compressor is communicated with the bottom of the carbonization tank; \| The carbon fixing and sealing unit comprises a slag discharging pump, a filter and a mixer, wherein the input end of the slag discharging pump is communicated with the bottom of the carbonization tank, the output end of the slag discharging pump is communicated with the filter, the upper end of the filter is communicated with the mixer, the upper end of the mixer is communicated with the output end of a sea water pump through a water flow pipeline, and the lower end of the mixer is provided with a water outlet which is communicated with a water flow pipeline leading to a deep sea discharge area; \| The limestone slurry pulping and filling unit comprises a limestone slurry pond, wherein the upper part of the limestone slurry pond is respectively communicated with the limestone powder bin and the output end of the seawater pump, and the bottom of the limestone slurry pond is communicated with the upper part of the carbonization tank. \|[0008] Preferably, the bottom of the temperature reduction tower is communicated with the bottom of the absorption tower through an airflow pipeline, and a booster fan is arranged on the airflow pipeline between the temperature reduction tower and the absorption tower.\|[0009] Preferably, the amine liquid circulation unit further comprises a rich liquid pump and a lean liquid pump, wherein the input end of the rich liquid pump is communicated with the bottom of the absorption tower, the output end of the rich liquid pump is communicated with a rich liquid inlet of the lean-rich liquid heat exchanger, the input end of the lean liquid pump is communicated with the bottom of the desorption tower, and the output end of the lean liquid pump is communicated with a lean liquid inlet of the lean-rich liquid heat exchanger.\|[0010] Preferably, a pressure reducing valve is arranged on the air flow pipeline between the air outlet and the compressor.\|[0011] Preferably, a bubble distributor and a stirrer are arranged in the carbonization tank, and the bubble distributor is communicated with the output end of the compressor.\|[0012] Preferably, the bottom of the filter is communicated with the limestone slurry pond, the upper end of the filter is also provided with a gas outlet, and the gas outlet is communicated with the input end of the compressor through a gas flow pipeline.\|[0013] The invention also provides a method for capturing and storing carbon by adopting the carbon capturing and storing system, which specifically comprises the following steps:\| S1, when waste gas needs decarburization treatment, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, the temperature is reduced to 40-60 ℃, the waste gas flows into the absorption tower from the bottom of the absorption tower, contacts with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, so that rich amine liquid and relatively pure gas are formed, and the relatively pure gas flows out from a gas outlet; \| S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid from the top of the desorption tower to the bottom of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a reboiler, desorbing carbon dioxide gas and forming lean amine liquid; \| S3, forming lean amine liquid, cooling the lean amine liquid twice through a lean-rich liquid heat exchanger and a lean liquid cooler, conveying the lean amine liquid to the top in an absorption tower, simultaneously, cooling the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing the cooled lean amine liquid to 4-6bar through a compressor, conveying the cooled lean amine liquid to the bottom of a carbonization tank, then, reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition based on a reinforced rock weathering principle to generate soluble calcium bicarbonate, conveying part of unreacted carbon dioxide gas to the compressor from an air outlet at the top of the carbonization tank, and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again; \| S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter for filtering to form clarified liquid and limestone slurry slag, conveying limestone powder and seawater into a limestone slurry tank to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank; \| s5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater in proportion to form mixed liquid with a pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, and conveying limestone slurry residues in the filter into a limestone slurry tank for preparing limestone slurry. \|[0014] Preferably, in S2, the two cooling steps of the formed lean amine solution include cooling to 60-70 ℃ by a lean-rich solution heat exchanger and cooling to 30-45 ℃ by a lean solution cooler.\|[0015] Preferably, in S5, the ratio of clarified liquid to seawater is 1 (10-1000).\|[0016] Compared with the prior art, the invention has the advantages that:\| (1) The invention provides a carbon capture storage system and a carbon capture storage method, wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine, then resolving the carbon dioxide gas in a desorption tower, then reacting the resolved carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, and finally sealing the calcium bicarbonate in a deep sea discharge area; compared with the traditional carbon fixation method of carbon dioxide through compression, liquefaction and transportation and underground salty water layer sealing, the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short, high-pressure and low-temperature high-energy equipment is not needed in the carbon capture and sealing process, the low-temperature storage and transportation of captured carbon dioxide gas are not needed, the energy consumption can be reduced, the carbon fixation cost can be saved, the phenomenon of carbon dioxide escape in the storage and transportation process can be avoided, the carbon fixation efficiency is improved, meanwhile, the consumption in the aspects of manpower and material resources can be reduced, and the problems of overlong carbon capture and sealing flow, high energy consumption, high cost, high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved. \|[0017] (2) The carbon capture storage system and the carbon capture storage method provided by the invention are characterized in that the carbon capture storage method is used for converting the resolved carbon dioxide gas and limestone slurry into calcium bicarbonate under an acidic condition, and the calcium bicarbonate can exist stably in the form of bicarbonate ions and calcium ions under deep sea and low temperature conditions, so that the carbon capture storage method can realize the purpose of permanently fixing carbon.\|DRAWINGS DESCRIPTION\|[0018] The invention is further described below with reference to the accompanying drawings and examples:\| FIG. 1 is a schematic diagram of a carbon capture storage system according to the present invention; \| The device comprises a temperature reduction tower, a2 absorption tower, a3 bypass valve, a 4 sea water pump, a 5 sea water outlet, a 6, an exhaust port, a7, a desorption tower, a 8, a lean-rich liquid heat exchanger, a9, a reboiler, a 10, a lean liquid cooler, a 11, a regenerated gas cooler, a 12, a compressor, a 13, a carbonization tank, a 14, an air outlet, a 15, a slag discharge pump, a 16, a filter, a 17, a mixer, a 18, a water outlet, a 19, a PH meter, a 20, a limestone slurry pond, a 21, a limestone powder warehouse, a 22, a booster fan, a 23, a rich liquid pump, a 24, a lean liquid pump, a 25, a pressure reducing valve, a 26, a bubble distributor, a 27, a stirrer, a 28, a gas outlet, a 29 and a limestone slurry pump. \|INVENTION MODE\|Detailed Description\|[0019] The following describes the present invention in further detail with reference to specific examples:\| A carbon capturing and storing system is shown in fig. 1, and comprises an exhaust gas absorbing unit, an amine liquid circulating unit, a carbon dioxide gas salinization unit and a carbon fixation and sealing unit which are sequentially communicated, wherein the carbon capturing and storing system also comprises a limestone slurry pulping and filling unit, and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. \|[0020] The waste gas absorption unit comprises a temperature reduction tower 1 and an absorption tower 2; the upper part of the temperature reduction tower 1 is communicated with a flue gas source through a flue gas conveying pipeline, and a bypass valve 3 is arranged on the flue gas conveying pipeline between the temperature reduction tower 1 and the flue gas source; the bypass valve 3 is opened to convey the waste gas to be decarbonized into the temperature reduction tower 1 for cooling treatment, a seawater spray device is arranged at the upper end of the interior of the temperature reduction tower 1, the seawater spray device is connected with the output end of a seawater pump 4 positioned outside the temperature reduction tower 1 through a water pipeline, the seawater is conveyed into the temperature reduction tower 1, the upper end of the temperature reduction tower 1 sprays the waste gas to the bottom of the temperature reduction tower 1 and fully contacts and mixes the waste gas conveyed into the temperature reduction tower 1 to further reduce the temperature of the waste gas, the bottom of the temperature reduction tower 1 is communicated with the absorption tower 2 and is used for conveying the waste gas subjected to the spray cooling treatment into the absorption tower 2, a seawater outlet 5 is also arranged at the bottom of the temperature reduction tower 1, a water pipeline leading to a seawater discharge area is connected at the seawater outlet 5 and is used for discharging the seawater sprayed to the bottom of the temperature reduction tower 1 into the sea, a lean amine liquid spray device is arranged at the upper end of the absorption tower 2 and is used for spraying the lean amine liquid from the upper end of the absorption tower 2 to a filler position close to the bottom of the absorption tower 2 and is fully contacted with the waste gas conveyed into the absorption tower 2, the waste gas is further reduced in temperature, the bottom of the absorption tower 2 is in contact with the waste gas is formed by the pure amine gas and the pure amine gas is discharged into the absorption tower 2 through the clean gas after the absorption tower 2 is relatively connected to the top of the absorption tower 2 through the clean gas which is relatively arranged to the top of the absorption tower 2, and the booster fan 22 is further arranged on the airflow pipeline between the temperature reduction tower 1 and the absorption tower 2 and is used for increasing the pressure of the waste gas conveyed into the absorption tower 2, increasing the flow speed and the airflow energy of the waste gas, and fully mixing the waste gas with the lean amine liquid in the absorption tower 2, so that the carbon dioxide gas in the waste gas fully contacts with the lean amine liquid and is absorbed by the lean amine liquid, and capturing the carbon dioxide gas in the waste gas is realized.\|[0021] The amine liquid circulation unit comprises a desorption tower 7, a lean-rich liquid heat exchanger 8 and a reboiler 9, wherein the reboiler 9 is communicated with the desorption tower 7 and is connected to a position close to the bottom of the desorption tower 7, namely a filler, a rich liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the absorption tower 2, a rich liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the desorption tower 7 and is used for heating the rich amine liquid at the bottom of the absorption tower 2 and then conveying the rich amine liquid to the top of the desorption tower 7, a spraying device at the top of the desorption tower 7 is used for spraying the rich amine liquid close to the bottom of the desorption tower 7 from the top of the desorption tower 7, the rich amine liquid sprayed to the filler absorbs steam heat generated by the reboiler 9 and then heats and desorbs carbon dioxide to form lean amine liquid containing only a small amount of carbon dioxide, and flows to the bottom of the desorption tower 7, a lean liquid inlet of the lean-rich liquid heat exchanger 8 is communicated with the bottom of the desorption tower 7, a lean liquid outlet of the lean-rich liquid heat exchanger 8 is communicated with the top of the absorption tower 2 through a lean liquid cooler 10 and is used for cooling the lean liquid at the bottom of the absorption tower 2, and is conveyed to the top of the absorption tower 2 from the lean liquid heat exchanger 8 to the top of the absorption tower 2 through the lean liquid heat exchanger 10 and then is recycled to the absorption tower 2. In order to ensure continuous and stable mutual circulation and transportation of the rich amine liquid and the lean amine liquid formed in the absorption tower 2 and the desorption tower 7 so as to achieve the effect of recycling the organic amine liquid, the amine liquid circulation unit further comprises a rich liquid pump 23 and a lean liquid pump 24, wherein the input end of the rich liquid pump 23 is communicated with the bottom of the absorption tower 2, the output end of the rich liquid pump is communicated with the rich liquid inlet of the lean-rich liquid heat exchanger 8 and is used for pumping the rich amine liquid formed in the absorption tower 2 into the lean-rich liquid heat exchanger 8 and transporting the rich amine liquid into the desorption tower 7, and similarly, the input end of the lean liquid pump 24 is communicated with the bottom of the desorption tower 7, and the output end of the rich liquid pump 24 is communicated with the lean liquid inlet of the lean-rich liquid heat exchanger 8.\|[0022] The carbon dioxide gas salinization unit comprises a regeneration gas cooler 11, a compressor 12 and a carbonization tank 13, wherein the input end of the regeneration gas cooler 11 is communicated with the top of the desorption tower 7, the output end of the regeneration gas cooler is communicated with the input end of the compressor 12, the output end of the compressor 12 is communicated with the bottom of the carbonization tank 13, carbon dioxide gas desorbed in the desorption tower 7 is cooled by the regeneration gas cooler 11, dehydrated and then flows into the compressor 12, the compressor 12 is pressurized and then is conveyed into the carbonization tank 13, and based on the rock weathering principle, the carbon dioxide gas and limestone slurry in the carbonization tank 13 are mixed and react under the acidic condition to form soluble calcium bicarbonate. In order to sufficiently mix and sufficiently react the carbon dioxide gas with the limestone slurry in the carbonization tank 13, a bubble distributor 26 and a stirrer 27 may be provided in the carbonization tank 13, the bubble distributor 26 may be connected to the output end of the compressor 12, the carbon dioxide gas supplied into the carbonization tank 13 by the compressor 12 may be separated into fine bubbles by the bubble distributor 26, the dissolution efficiency of the carbon dioxide gas in the limestone slurry may be improved, the contact ratio of the carbon dioxide gas with the limestone slurry may be increased, and the reaction efficiency may be improved, and the carbon dioxide gas and the limestone slurry in the carbonization tank 13 may be sufficiently mixed and reacted with each other by stirring by the stirrer 27, thereby further improving the conversion rate of the carbon dioxide.\|[0023] The carbon sequestration unit comprises a deslagging pump 15, a filter 16 and a mixer 17, wherein the input end of the deslagging pump 15 is communicated with the bottom of the carbonization tank 13, the output end of the deslagging pump 15 is communicated with the filter 16 and is used for conveying soluble calcium bicarbonate and limestone slurry generated by the reaction at the bottom of the carbonization tank 13 into the filter 16 together for filtering, the upper end of the filter 16 is communicated with the mixer 17, the upper end of the mixer 17 is communicated with the output end of the sea water pump 4 through a water flow pipeline, the lower end of the mixer 17 is provided with a water outlet 18, the water outlet 18 is communicated with a water flow pipeline leading to a deep sea discharge area, the clarified liquid separated from the filter 16 is conveyed into the mixer 17 and is mixed with sea water from the sea water pump 4 in the mixer 17 to form mixed liquid, then the mixed liquid is discharged into the deep sea discharge area through the water flow pipeline to achieve the purpose of permanently sequestration, and a PH meter 19 is further arranged at the water outlet 18 and is used for monitoring the PH value of the mixed liquid and the sea water, and the clear liquid is discharged into the deep sea after the PH value of the clear liquid meets the requirements. The upper end of the filter 16 is also provided with a gas outlet 28, and the gas outlet 28 is communicated with the input end of the compressor 12 through a gas flow pipeline and is used for conveying the carbon dioxide gas which is conveyed into the filter 16 together with the soluble calcium bicarbonate and limestone slurry into a carbon dioxide gas salinization unit for continuous salinization.\|[0024] The limestone slurry pulping and filling unit comprises a limestone slurry pond 20, wherein the upper part of the limestone slurry pond 20 is respectively communicated with a limestone powder bin 21 and the output end of a sea water pump 4, and is used for adding superfine limestone powder and sea water in the limestone powder bin 21 into the limestone slurry pond 20 together and uniformly mixing the superfine limestone powder and the sea water in the limestone slurry pond 20 to form limestone slurry, a stirrer 27 is further arranged in the limestone slurry pond 20, stirring is performed by adopting the stirrer 27 in the process of adding the limestone powder and the sea water into the limestone slurry pond 20, so that rapid uniform mixing of the limestone powder and the sea water is facilitated, the bottom of the limestone slurry pond 20 is communicated with the upper part of a carbonization tank 13 through a slurry conveying pipeline, a limestone slurry pump 29 is arranged on the slurry conveying pipeline, and the limestone slurry in the limestone slurry pond 20 is pumped into the carbonization tank 13 through the limestone slurry pump 29 to perform internal reaction. The bottom of the filter 16 is also communicated with the limestone slurry pond 20, and limestone sediment formed at the lower layer in the filter 16 is conveyed into the limestone slurry pond 20 and is used as a raw material together with superfine limestone powder to prepare limestone slurry.\|[0025] The method for capturing and storing carbon by adopting the carbon capturing and storing system specifically comprises the following steps:\| S1, when the waste gas needs to be decarbonized, a bypass valve is opened, the waste gas is conveyed into a temperature reduction tower through a flue gas conveying pipeline to be sprayed with seawater, seawater sprayed through a Wen Dana is fully contacted with the flue gas and absorbs heat brought by the flue gas, so that the flue gas is cooled to be within a range of 40-60 ℃, then, the waste gas flows into the absorption tower from the bottom of the absorption tower, is contacted with lean amine liquid sprayed in the absorption tower and is absorbed by the lean amine liquid, rich amine liquid and relatively pure gas are formed, and the relatively pure gas is discharged into the atmosphere from an exhaust port at the top of the absorption tower or is conveyed to a subsequent gas treatment unit. Wherein, the flue gas is conveyed into a temperature reduction tower according to the gas flow of 50-500L/h, the lean amine liquid in the absorption tower can be one of aqueous solution or mixed aqueous solution of a plurality of methyl diethanolamine, ethanolamine, triethylene tetramine and the like, and the concentration of carbon dioxide gas in the relatively pure gas is below 2.0 percent (mole percent). \|[0026] S2, heating the formed rich amine liquid to 95-110 ℃ through a lean-rich liquid heat exchanger, then conveying the rich amine liquid to the top of a desorption tower, spraying the rich amine liquid to the bottom from the top of the desorption tower, heating the rich amine liquid after absorbing steam heat generated by a bottom reboiler, desorbing carbon dioxide gas, forming lean amine liquid, and flowing to the bottom of the desorption tower.\|[0027] S3, cooling the lean amine liquid at the bottom of the desorption tower to 60-70 ℃ through a lean-rich liquid heat exchanger, cooling to 30-45 ℃ through a lean liquid cooler, conveying the lean amine liquid to the top of the absorption tower, spraying the lean amine liquid to the bottom of the absorption tower from the top in the absorption tower, simultaneously, cooling and dewatering the desorbed carbon dioxide gas through a regenerated gas cooler, pressurizing to 4-6bar through a compressor, and conveying the carbon dioxide gas to the bottom of a carbonization tank, and then, based on the reinforced rock weathering principle, absorbing and reacting the desorbed carbon dioxide gas with limestone slurry under an acidic condition to generate soluble calcium bicarbonate, wherein the reaction equation is as follows: And conveying part of unreacted carbon dioxide gas to a compressor from an air outlet at the top of the carbonization tank, compressing and conveying the compressed carbon dioxide gas to the bottom of the carbonization tank again. \|[0028] S4, starting a slag discharge pump, conveying the generated calcium bicarbonate and limestone slurry at the bottom of the carbonization tank into a filter according to the flow ratio of 5-100L/h for filtering to form clarified liquid and limestone slurry slag, simultaneously conveying limestone powder and seawater into a limestone slurry pond to prepare limestone slurry, starting a limestone slurry pump, and conveying the limestone slurry to the top of the carbonization tank according to the flow ratio of 5-100L/h.\|[0029] S5, conveying clarified liquid formed in the filter into a mixer, mixing the clarified liquid with seawater according to the proportion of 1 (10-1000), forming mixed liquid with the pH value not less than 6, discharging the mixed liquid to a deep sea discharge area through a discharge outlet, achieving the purpose of carbon fixation and sealing, and conveying limestone slurry slag in the filter into a limestone slurry pond for preparing limestone slurry.\|[0030] Compared with the traditional carbon fixation method for sealing and storing carbon dioxide through compression, liquefaction and transportation and an underground salty water layer, the carbon capture and storage method does not need high-pressure and low-temperature high-energy equipment, low-temperature storage and transportation, saves the cost consumed in the low-temperature storage, transportation and sealing and storage processes, avoids the carbon dioxide escaping phenomenon in the transportation process, greatly shortens the carbon fixation process, and reduces the carbon fixation energy consumption. In addition, because the calcium bicarbonate exists in the form of bicarbonate ions and calcium ions in the sea water and can exist stably under deep sea and low temperature conditions, the carbon capturing and storing method can better achieve the purpose of carbon fixation and sealing.\|[0031] The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and implement the same according to the content of the present invention, and are not intended to limit the scope of the present invention. It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof, and it is therefore desired that the present invention be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.	Family Number\|(113778323)\|113778323\|Object of Invention\|(CN119607861 A)\|The invention provides a carbon capture storage system and a carbon capture storage method , which are used for solving the problems of overlong carbon capture sealing process , high energy consumption , high cost , large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art . Disclosure of InventionThe invention aims to provide a carbon capture storage system and a carbon capture storage method , which are used for solving the problems of overlong carbon capture sealing process , high energy consumption , high cost , large manpower and material resource consumption and the like of the existing organic amine decarburization storage method in the prior art . \|The invention relates to the technical field of flue gas treatment , in particular to a carbon capture storage system and a carbon capture storage method . \|The invention relates to the technical field of flue gas treatment , in particular to a carbon capturing and storing system and a carbon capturing and storing method , comprising an exhaust gas absorbing unit , an amine liquid circulating unit , a carbon dioxide gas salifying unit and a carbon fixing and sealing unit which are sequentially communicated ; the device also comprises a limestone ( . . . ) \|Abstract\|(CN119607861 A)\|The invention relates to the technical field of flue gas treatment , in particular to a carbon capture and storage system and a carbon capture and storage method . The carbon capture and storage system comprises a waste gas absorption unit , an amine liquid circulation unit , a carbon dioxide gas salinization unit and a carbon sequestration unit which are communicated in sequence ; the system further comprises a limestone slurry pulping and filling unit ; and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit . The carbon capture and storage method is a brand - new organic amine decarburization and permanent carbon sequestration method provided on the basis of the principle of enhancing rock weathering ; compared with a traditional carbon sequestration method that carbon dioxide is transported through compression and liquefaction and stored in an underground salt water layer , the method has the advantages that the carbon capturing and storing process is short , high - pressure and low - temperature high - energy - consumption equipment does not need to be used , the captured carbon dioxide gas does not need to be stored and transported at low temperature , energy consumption can be reduced , the carbon sequestration cost is saved , and the carbon sequestration efficiency is improved . The carbon dioxide escape phenomenon in the storage and transportation process can be avoided , and the carbon sequestration efficiency is improved . \|Title\|(CN119607861 A)\|Carbon capture and storage system and carbon capture and storage method \|Advantages / Prev. Drawbacks\|(CN119607861 A)\|Compared with the prior art , the invention has the advantages that : ( 1 ) The invention provides a carbon capture storage system and a carbon capture storage method , wherein the carbon capture storage method is a brand new organic amine decarburization and permanent carbon fixation method based on the enhanced rock weathering principle ; the carbon capturing and storing method comprises the steps of firstly capturing carbon dioxide gas in flue gas through organic amine , then resolving the carbon dioxide gas in a desorption tower , then reacting ( . . . ) method of carbon dioxide through compression , liquefaction and transportation and underground salty water layer sealing , the carbon capture and storage method has the advantages that the carbon capture and sealing flow is short , high - pressure and low - temperature high - energy equipment is not needed in the carbon capture and sealing process , the low - temperature storage and transportation of captured carbon dioxide gas are not needed , the energy consumption can be reduced , the carbon fixation cost can be saved , the phenomenon ( . . . ) meanwhile , the consumption in the aspects of manpower and material resources can be reduced , and the problems of overlong carbon capture and sealing flow , high energy consumption , high cost , high manpower and material resource consumption and the like in the traditional organic amine decarburization storage method in the prior art are solved . \|Independent Claims\|(CN119607861 A)\|1. The carbon capturing and storing system is characterized by comprising an exhaust gas absorbing unit , an amine liquid circulating unit , a carbon dioxide gas salinization unit , a carbon fixation and sealing unit and a limestone slurry pulping and filling unit ; ( . . . ) \|	Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-053/96\|B01D-2258/0283\|C01B-032/55		B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-053/96\|B01D-2258/0283\|C01B-032/55	B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-053/96\|C01B-032/55	B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-053/96\|C01B-032/55			CN119838413	CN119838413 114246229 WHO=Examiner SELF=N CAT=A						PENDING	(CN119607861)\|PENDING	ALIVE	(CN119607861)\|ALIVE	(CN119607861)\|LEGAL DETAILS FOR CN119607861\|Actual or expected expiration date=2044-12-31\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-12-31\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202411977823\|Application date=2024-12-31\|Standardized application number=2024CN-1977823\|Event publication date=2025-03-14\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN119607861\|Publication stage code=A\|Publication date=2025-03-14\|Standardized publication number=CN119607861\|Event publication date=2025-03-14\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2025-04-01\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN119607861)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTcM0PYETPPhlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000076748113&ekey=2056&xpn=CN119607861&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=X3YLgN33UC9MvSpo4Kvsq5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN119607861)\|CN	(CN119607861)\|NAME=SINOTECH ENERGY CO., LTD. , COUNTRY=CN				(CN119607861)\|NAME=WEI YING\|NAME=HE WEI	(CN119607861)\|1	1	1					(CN119607861)\|Number of Claims: NCL=9\|Gazette date: GAZDATE=2025-03-14\|Gazette number: GAZNUM=41-1102\|Number of Pages: NPAGES=10\|		(CN119607861)\|CHINESE (CHI)	(CN119607861)\|Patent	Titre: (CN119607861)\|Carbon capture and storage system and carbon capture and storage method Résumé: (CN119607861)\|The invention relates to the technical field of flue gas treatment, in particular to a carbon capture and storage system and a carbon capture and storage method.The carbon capture and storage system comprises a waste gas absorption unit, an amine liquid circulation unit, a carbon dioxide gas salinization unit and a carbon sequestration unit which are communicated in sequence; the system further comprises a limestone slurry pulping and filling unit; and the limestone slurry pulping and filling unit is communicated with the carbon dioxide gas salinization unit. The carbon capture and storage method is a brand-new organic amine decarburization and permanent carbon sequestration method provided on the basis of the principle of enhancing rock weathering; compared with a traditional carbon sequestration method that carbon dioxide is transported through compression and liquefaction and stored in an underground salt water layer, the method has the advantages that the carbon capturing and storing process is short, high-pressure and low-temperature high-energy-consumption equipment does not need to be used, the captured carbon dioxide gas does not need to be stored and transported at low temperature, energy consumption can be reduced, the carbon sequestration cost is saved, and the carbon sequestration efficiency is improved. The carbon dioxide escape phenomenon in the storage and transportation process can be avoided, and the carbon sequestration efficiency is improved.	5	Abstract	gpt-4o-mini	no	The article focuses on a carbon capture and storage system related to flue gas treatment, which does not align with the topic of enhanced weathering and mineral carbonation.
7	AU2007900853\|AU2007902727\|AU2007906379\|AU2008217572\|WOAU2008/000232\|AU2009250983	WOAU2008/000232\|AU2009250983\|IN6026/DELNP/2009\|CA2678800\|KR10-2009-7019662\|CN200880006610\|JP2009550646\|US12/527,608\|EP08706115\|AU2008217572	IN293376\|CA2678800\|KR10-1527365\|CN101641145\|JP5345954\|US8496897\|EP2134449\|IN6026/DELNP/2009\|EP2134449\|JP2010519027\|AU2008217572\|CN101641145\|US20100021362\|AU2009250983\|EP2134449\|KR10-2009-0125109\|AU2008217572\|CA2678800\|WO2008/101293	6597398	WO2008/101293 A1 2008-08-28 [WO2008101293]\|AU2009250983 A1 2010-01-14 [AU2009250983]\|IN293376 B 2018-02-26 [IN-293376]\|IN6026/DELNP/2009 A 2011-08-26 [IN2009DN06026]\|CA2678800 C 2015-11-24 [CA2678800]\|CA2678800 A1 2008-08-28 [CA2678800]\|KR10-1527365 B1 2015-06-22 [KR101527365]\|KR10-2009-0125109 A 2009-12-03 [KR20090125109]\|CN101641145 B 2014-05-07 [CN101641145B]\|CN101641145 A 2010-02-03 [CN101641145]\|JP5345954 B2 2013-11-20 [JP5345954]\|JP2010519027 A 2010-06-03 [JP2010519027]\|US8496897 B2 2013-07-30 [US8496897]\|US20100021362 A1 2010-01-28 [US20100021362]\|EP2134449 B1 2012-10-10 [EP2134449]\|EP2134449 A4 2011-03-30 [EP2134449]\|EP2134449 A1 2009-12-23 [EP2134449]\|AU2008217572 B2 2010-02-04 [AU2008217572]\|AU2008217572 A1 2008-08-28 [AU2008217572]	2007-02-20\|2007-05-22\|2007-11-21\|2008-02-20\|2009-12-16	2008-02-20\|2009-12-16\|2009-09-18\|2008-02-20\|2008-02-20\|2008-02-20\|2008-02-20\|2008-02-20\|2008-02-20\|2008-02-20	2018-02-26\|2015-11-24\|2015-06-22\|2014-05-07\|2013-11-20\|2013-07-30\|2012-10-10\|2011-08-26\|2011-03-30\|2010-06-03\|2010-02-04\|2010-02-03\|2010-01-28\|2010-01-14\|2009-12-23\|2009-12-03\|2008-08-28\|2008-08-28\|2008-08-28	(EP2134449)\|2012-10-10\|(US8496897)\|2013-07-30\|\|(JP5345954)\|2013-11-20\|(CN101641145B)\|2014-05-07\|(IN-293376)\|2018-02-26\|(CA2678800)\|2015-11-24\|(KR101527365)\|2015-06-22\|(AU2008217572)\|2010-02-04\|	(EP2134449)\|2018-10-31\|(US8496897)\|2021-09-06\|(WO2008/101293)\|2010-08-20\|(JP5345954)\|2018-08-23\|(CN101641145)\|2018-02-20\|(IN293376)\|2028-02-20\|(CA2678800)\|2019-02-20\|(KR10-1527365)\|2018-06-04\|(AU2008217572)\|2018-09-13\|(AU2009250983)\|2010-12-02	(EP2134449)\|System, apparatus and method for carbon dioxide sequestration	(EP2134449)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.	HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD ([AU])\|RICHARD J HUNWICK\|HUNWICK, RICHARD J.\|HUNWICK RICHARD J.\|HUNWICK RICHARD J. ([AU])\|Richard Jay Han Wick\|HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD J ([AU])\|HUNWICK RICHARD J ([AU])	(EP2134449)\|Hunwick, Richard J. ([AU])\|(EP2134449)\|Hunwick, Richard J. ([AU])\|(EP2134449)\|Hunwick, Richard J. ([AU])\|(US8496897)\|Hunwick Richard J ([AU])\|(US20100021362)\|HUNWICK RICHARD J\|(WO2008/101293)\|HUNWICK, Richard J. ([AU])\|(JP5345954)\|Richard Jay Han Wick\|(JP2010519027)\|Richard Jay Han Wick\|(CN101641145)\|HUNWICK RICHARD J. ([AU])\|(CN101641145)\|HUNWICK RICHARD J. ([AU])\|(IN293376)\|RICHARD J HUNWICK\|(IN6026/DELNP/2009)\|RICHARD J HUNWICK ([AU])\|(CA2678800)\|HUNWICK, RICHARD J. ([AU])\|(CA2678800)\|HUNWICK, RICHARD J. ([AU])\|(KR10-1527365)\|HUNWICK RICHARD J.\|(KR10-2009-0125109)\|HUNWICK RICHARD J.\|(AU2008217572)\|HUNWICK, RICHARD J.\|(AU2008217572)\|RICHARD HUNWICK\|(AU2009250983)\|HUNWICK, RICHARD	HUNWICK RICHARD J	(EP2134449)\|Hunwick, Richard J.\|(EP2134449)\|Hunwick, Richard J.\|(EP2134449)\|Hunwick, Richard J.	(EP2134449)\|Williams, Richard Andrew Norman;Harrison Goddard Foote ([GB])\|Reg. Nb: 100754772\|(US8496897)\|Frommer Lawrence & Haug LLP\|Santucci Ronald R\|(WO2008/101293)\|GRIFFITH HACK ([AU])\|(JP5345954)\|YOSHIDA Kenji\|Reg. Nb: 100075258\|ISHIDA Jun\|Reg. Nb: 100096976\|(CN101641145)\|CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11314\|(CA2678800)\|MBM INTELLECTUAL PROPERTY LAW LLP ([CA])\|(KR10-2009-0125109)\|HALLA PATENT & LAW FIRM	(EP2134449)\|A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor.\|It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations.\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\|Should it arise that the content of limestone or dolomite in the coal fuel is inadequate for the duty (as is likely to be the case with most power station fly ashes), it is possible to dose the appropriate quantity of pulverised limestone or dolomite to the power station boilers (not shown).\|The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s).\|	(EP2134449)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) in a third stage, passing the reactive slurry from (ii) through a reactor (52,70) that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|16. A system for (10) sequestering carbon dioxide from a gas stream, the system for comprising: (a) a first apparatus (28,30) for removing the carbon dioxide from the gas stream and for absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and (b) a reactor (52,70) for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|	(EP2134449)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|In accordance with a second aspect, the present invention provides a system for sequestering carbon dioxide from a gas stream, the system comprising: (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and (b) a reactor for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|	(EP2134449)\|METHANEDIONE(100,65)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,11)\|SEQUESTRATION(100,8)\|METHANEDIONE SEQUESTRATION(100,7)\|REACTION SLURRY(77,25)\|AMMONIATED SLURRY(70,6)\|METAL SILICATE(63,40)\|METAL SILICATE SLURRY(63,34)\|LIMESTONE PULVERIZATION(60,1)\|METHANEDIONE ISOLATION(56,1)\|REACTOR(50,25)\|METHANEDIONE CONVERSION(48,1)\|PERMANENT SEQUESTRATION(41,2)\|COAL FUEL(38,1)\|PRESSURIZED AMMONIA(36,1)\|AMMONIA(35,78)\|ABSORBED METHANEDIONE(34,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(34,1)\|METAL CARBONATE(32,12)\|NATURALLY OCCURRING SINK(30,1)\|PIPELINE(29,27)\|SCRUBBING CHAMBER(29,19)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|REACTION ENHANCEMENT(25,6)\|DOLOMITE(25,4)\|CHILLED SLURRY(25,3)\|SLURRY(23,41)\|AMMONIA ABSORPTION CHILLER(23,2)\|AMMONIA RECOVERY VESSEL(22,14)\|UNDERGROUND CHAMBER(22,10)\|EVAPORATION CHAMBER(21,1)\|REACTOR CONTROL(21,1)\|FLOW PATH(20,14)\|POWER STATION BOILER(20,1)\|MAGNESIUM SILICATE(18,2)\|AMMONIA WATER(17,18)\|METAL SILICATE ROCK(17,2)\|DUTY(15,2)\|OVERLAND AMMONIA PIPELINE(14,2)\|CARBON CAPTURE(13,1)\|METAL CARBONATE PRODUCT(12,4)\|CHILLED AMMONIA WATER(12,3)\|RESIDUAL AMMONIA SCRUBBER(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|RESULTANT AMMONIA WATER(12,1)\|FLY ASH(11,7)\|AMMONIA ABSORPTION CHAMBER(11,5)\|POWER STATION FLY ASH(11,4)\|CENT METHANEDIONE(11,2)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|POWER STATION(10,24)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|SERPENTINE MG3SI2O(9,1)\|FLUE GAS(8,33)\|AMMONIA LOSS(8,4)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE REGENERATION(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|CARBONATION REACTION(7,2)\|CO2 ABSORBER(7,2)\|EVAPORATOR VESSEL(7,2)\|METHANEDIONE CONTENT(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|OLIVINE(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|ABSORBER AQ(6,1)\|AMMONIA STRIPPING(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTIVE SLURRY HEATING(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,4)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|WOLLASTONITE(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENT NITROGEN(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|LIQUID PRESSURIZATION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|WT SLURRY(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|SOX(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|\|(EP2134449)\|METHANEDIONE(100,65)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,11)\|SEQUESTRATION(100,8)\|METHANEDIONE SEQUESTRATION(100,7)\|REACTION SLURRY(77,25)\|AMMONIATED SLURRY(70,6)\|METAL SILICATE(63,40)\|METAL SILICATE SLURRY(63,34)\|LIMESTONE PULVERIZATION(60,1)\|METHANEDIONE ISOLATION(56,1)\|REACTOR(50,25)\|METHANEDIONE CONVERSION(48,1)\|PERMANENT SEQUESTRATION(41,2)\|COAL FUEL(38,1)\|PRESSURIZED AMMONIA(36,1)\|AMMONIA(35,78)\|ABSORBED METHANEDIONE(34,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(34,1)\|METAL CARBONATE(32,12)\|NATURALLY OCCURRING SINK(30,1)\|PIPELINE(29,27)\|SCRUBBING CHAMBER(29,19)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|REACTION ENHANCEMENT(25,6)\|DOLOMITE(25,4)\|CHILLED SLURRY(25,3)\|SLURRY(23,41)\|AMMONIA ABSORPTION CHILLER(23,2)\|AMMONIA RECOVERY VESSEL(22,14)\|UNDERGROUND CHAMBER(22,10)\|EVAPORATION CHAMBER(21,1)\|REACTOR CONTROL(21,1)\|FLOW PATH(20,14)\|POWER STATION BOILER(20,1)\|MAGNESIUM SILICATE(18,2)\|AMMONIA WATER(17,18)\|METAL SILICATE ROCK(17,2)\|DUTY(15,2)\|OVERLAND AMMONIA PIPELINE(14,2)\|CARBON CAPTURE(13,1)\|METAL CARBONATE PRODUCT(12,4)\|CHILLED AMMONIA WATER(12,3)\|RESIDUAL AMMONIA SCRUBBER(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|RESULTANT AMMONIA WATER(12,1)\|FLY ASH(11,7)\|AMMONIA ABSORPTION CHAMBER(11,5)\|POWER STATION FLY ASH(11,4)\|CENT METHANEDIONE(11,2)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|POWER STATION(10,24)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|SERPENTINE MG3SI2O(9,1)\|FLUE GAS(8,33)\|AMMONIA LOSS(8,4)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE REGENERATION(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|CARBONATION REACTION(7,2)\|CO2 ABSORBER(7,2)\|EVAPORATOR VESSEL(7,2)\|METHANEDIONE CONTENT(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|OLIVINE(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|ABSORBER AQ(6,1)\|AMMONIA STRIPPING(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTIVE SLURRY HEATING(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,4)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|WOLLASTONITE(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENT NITROGEN(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|LIQUID PRESSURIZATION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|WT SLURRY(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|SOX(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|\|(EP2134449)\|METHANEDIONE(100,65)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,11)\|SEQUESTRATION(100,8)\|METHANEDIONE SEQUESTRATION(100,7)\|REACTION SLURRY(77,25)\|AMMONIATED SLURRY(70,6)\|METAL SILICATE(63,40)\|METAL SILICATE SLURRY(63,34)\|LIMESTONE PULVERIZATION(60,1)\|METHANEDIONE ISOLATION(56,1)\|REACTOR(50,25)\|METHANEDIONE CONVERSION(48,1)\|PERMANENT SEQUESTRATION(41,2)\|COAL FUEL(38,1)\|PRESSURIZED AMMONIA(36,1)\|AMMONIA(35,78)\|ABSORBED METHANEDIONE(34,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(34,1)\|METAL CARBONATE(32,12)\|NATURALLY OCCURRING SINK(30,1)\|PIPELINE(29,27)\|SCRUBBING CHAMBER(29,19)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|REACTION ENHANCEMENT(25,6)\|DOLOMITE(25,4)\|CHILLED SLURRY(25,3)\|SLURRY(23,41)\|AMMONIA ABSORPTION CHILLER(23,2)\|AMMONIA RECOVERY VESSEL(22,14)\|UNDERGROUND CHAMBER(22,10)\|EVAPORATION CHAMBER(21,1)\|REACTOR CONTROL(21,1)\|FLOW PATH(20,14)\|POWER STATION BOILER(20,1)\|MAGNESIUM SILICATE(18,2)\|AMMONIA WATER(17,18)\|METAL SILICATE ROCK(17,2)\|DUTY(15,2)\|OVERLAND AMMONIA PIPELINE(14,2)\|CARBON CAPTURE(13,1)\|METAL CARBONATE PRODUCT(12,4)\|CHILLED AMMONIA WATER(12,3)\|RESIDUAL AMMONIA SCRUBBER(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|RESULTANT AMMONIA WATER(12,1)\|FLY ASH(11,7)\|AMMONIA ABSORPTION CHAMBER(11,5)\|POWER STATION FLY ASH(11,4)\|CENT METHANEDIONE(11,2)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|POWER STATION(10,24)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|SERPENTINE MG3SI2O(9,1)\|FLUE GAS(8,33)\|AMMONIA LOSS(8,4)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE REGENERATION(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|CARBONATION REACTION(7,2)\|CO2 ABSORBER(7,2)\|EVAPORATOR VESSEL(7,2)\|METHANEDIONE CONTENT(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|OLIVINE(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|ABSORBER AQ(6,1)\|AMMONIA STRIPPING(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTIVE SLURRY HEATING(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,4)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|WOLLASTONITE(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENT NITROGEN(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|LIQUID PRESSURIZATION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|WT SLURRY(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|SOX(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|\|(US8496897)\|METHANEDIONE SEQUESTRATION(100,16)\|SEQUESTRATION(100,10)\|METHANEDIONE SEQUESTRATION(100,9)\|ABSORPTION(100,3)\|AMMONIA ABSORPTION(100,3)\|AMMONIA ABSORPTION(100,2)\|REACTION SLURRY(73,27)\|METAL SILICATE SLURRY(70,35)\|PRESSURIZED AMMONIA(68,2)\|LIMESTONE PULVERIZATION(61,1)\|METHANEDIONE(59,59)\|METHANEDIONE ISOLATION(56,1)\|METAL SILICATE ROCK(54,5)\|AMMONIA RECOVERY(53,8)\|METHANEDIONE CONVERSION(48,1)\|PERMANENT SEQUESTRATION(42,2)\|EVAPORATOR(41,8)\|METAL SILICATE(40,35)\|SCRUBBING CHAMBER(39,21)\|COAL FUEL(39,1)\|AMMONIA(34,79)\|RECOVERY VESSEL(31,18)\|NATURALLY OCCURRING SINK(31,1)\|REACTOR(29,23)\|GAS STREAM(28,10)\|CHILLED AMMONIA WATER(28,5)\|PIPELINE(27,28)\|SLURRY(26,43)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|DOLOMITE(25,4)\|PYROXENE RICH MINERAL(24,2)\|AMMONIA RECOVERY VESSEL(22,14)\|AMMONIA LOSS(22,4)\|MAGNESIUM RICH SILICATE(21,5)\|EVAPORATION CHAMBER(21,1)\|AMMONIA WATER(20,19)\|POWER STATION BOILER(20,1)\|REACTION ENHANCEMENT(19,5)\|METAL CARBONATE(17,10)\|UNDERGROUND CHAMBER(16,10)\|DUTY(16,2)\|REACTOR CONTROL(16,2)\|PCT AU(15,1)\|RESIDUAL AMMONIA SCRUBBER(14,4)\|OVERLAND AMMONIA PIPELINE(14,2)\|CARBON CAPTURE(13,1)\|FLY ASH(12,7)\|OLIVINE(12,5)\|AMMONIATED SLURRY(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|FLOW PATH(11,9)\|AMMONIA ABSORPTION CHAMBER(11,5)\|POWER STATION FLY ASH(11,4)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|PUBLICATION NUMBER(11,1)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE CAPTURE(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CO2 ABSORBER(9,3)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|FLUE GAS(8,33)\|POWER STATION(8,24)\|METAL CARBONATE PRODUCT(8,3)\|CHILLED SLURRY(8,2)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|METHANEDIONE CONTENT(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|PRETREATMENT HARD CRUSHING(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|EVAPORATOR VESSEL(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|AMMONIA STRIPPING(6,1)\|DENSER SLURRY(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PIPELINE VELOCITY(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|MAGNESIUM ION(5,2)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA ABSORPTION CHILLER(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|CORE CARBONATION REACTION(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SILICATE SLURRY DENSITY(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,5)\|MWE(4,5)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|MG3SI2O(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|LIQUID PRESSURIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|T WT SLURRY(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|SOX(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BEDROCK(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|\|(US20100021362)\|AMMONIA(100,84)\|METHANEDIONE(100,67)\|SLURRY(100,43)\|METAL SILICATE SLURRY(100,37)\|PIPELINE(100,30)\|REACTION SLURRY(100,27)\|AMMONIA WATER(100,20)\|METHANEDIONE SEQUESTRATION(100,16)\|FLOW PATH(100,14)\|GAS STREAM(100,12)\|SEQUESTRATION(100,10)\|METHANEDIONE SEQUESTRATION(100,9)\|CARBON SEQUESTRATION(100,8)\|ABSORPTION(100,4)\|METAL SILICATE ROCK(100,4)\|METAL SILICATE ROCK SLURRY(100,4)\|CARBON SEQUESTRATION(100,3)\|AMMONIA ABSORPTION(100,2)\|FLOW PATH PROVISION(100,1)\|LIMESTONE PULVERIZATION(61,1)\|METAL SILICATE(59,41)\|METHANEDIONE ISOLATION(56,1)\|AMMONIATED SLURRY(54,5)\|METHANEDIONE CONVERSION(48,1)\|MAGNESIUM RICH SILICATE(47,7)\|REACTOR(42,27)\|PERMANENT SEQUESTRATION(42,2)\|METAL CARBONATE(40,14)\|EVAPORATOR(39,8)\|COAL FUEL(39,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(35,1)\|SCRUBBING CHAMBER(34,20)\|NATURALLY OCCURRING SINK(31,1)\|REACTION ENHANCEMENT(30,6)\|LIQUID PRESSURIZATION(28,2)\|INSOLUBLE CARBONATE(26,4)\|RETURN PATHWAY(26,2)\|POWER THIRSTY CLIMATE(26,1)\|DOLOMITE(25,4)\|CHILLED SLURRY(25,3)\|AMMONIA ABSORPTION CHILLER(23,2)\|AMMONIA RECOVERY VESSEL(22,14)\|AMMONIA LOSS(22,4)\|AMMONIA ABSORPTION CHAMBER(21,6)\|CHAMBER PRESSURIZATION(21,1)\|EVAPORATION CHAMBER(21,1)\|POWER STATION BOILER(20,1)\|UNDERGROUND CHAMBER(16,10)\|DUTY(16,2)\|REACTOR CONTROL(16,2)\|RESIDUAL AMMONIA SCRUBBER(14,4)\|OVERLAND AMMONIA PIPELINE(14,2)\|RECIRCULATION(14,2)\|CARBON CAPTURE(13,1)\|FLY ASH(12,7)\|OLIVINE(12,5)\|METAL CARBONATE PRODUCT(12,4)\|CHILLED AMMONIA WATER(12,3)\|LAGGED ABOVEGROUND PIPELINE(12,1)\|METHANEDIONE PERMANENT SEQUESTRATION(12,1)\|POWER STATION FLY ASH(11,4)\|ABSORBENT SLURRY DELUGING SPRAY(11,1)\|AMMONIA BUBBLE(10,3)\|MINERAL CARBONATION(10,3)\|HUNTER VALLEY(10,2)\|METHANEDIONE CAPTURE(10,2)\|METHANEDIONE SINK(10,2)\|RESIDUAL METHANEDIONE SCRUBBER(10,1)\|EVAPORATOR CHAMBER(9,5)\|RETURN PIPELINE(9,5)\|CO2 ABSORBER(9,3)\|CARBONATED SILICATE SLURRY(9,1)\|METHANEDIONE TONNE(9,1)\|FLUE GAS(8,33)\|POWER STATION(8,24)\|HOT SILICATE SLURRY(8,2)\|INCOMING REACTIVE SLURRY(8,2)\|METHANEDIONE CONTENT(8,2)\|UNDERGROUND REACTOR(8,2)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|FINAL EMPLACEMENT REHABILITATION(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|METHANEDIONE SCRUBBING CHAMBER(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|RAW FLUE GAS(7,6)\|ELECTRICITY GENERATION PLANT(7,3)\|EVAPORATOR VESSEL(7,2)\|AMMONIA TONNE(7,1)\|BICARBONATE NH4HCO(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|INSOLUBLE MAGNESIA(7,1)\|MAXIMIZE REGENERATION(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|STACKED SUBCHAMBER(7,1)\|FLUE GAS FILTER(6,5)\|POWER STATION FLUE GAS(6,5)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE(6,3)\|AMMONIA STRIPPING(6,1)\|DENSER SLURRY(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|HARMFUL METHANEDIONE GAS(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|PIPELINE VELOCITY(6,1)\|PRESSURIZED AMMONIA PASS(6,1)\|RAW REACTIVE SLURRY(6,1)\|REDUCING METHANEDIONE EMISSION(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|MAGNESIUM ION(5,2)\|METHANEDIONE SOURCE(5,2)\|MINERAL MATTER(5,2)\|PUMPING ENERGY(5,2)\|SLURRY FEED(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA MILLION(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBONATE MINERAL(5,1)\|CONCENTRATED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|CORE CARBONATION REACTION(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|PYROXENE SILICATE METAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|RECOVERED AMMONIA(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SILICATE SLURRY DENSITY(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,5)\|MWE(4,5)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|MG3SI2O(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|KEEPING UP(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|T WT SLURRY(4,1)\|VAPORIZED AMMONIA FLOW(4,1)\|REACTION CHAMBER(3,4)\|METAL SILICATE SOLUTION(3,3)\|STEAM(3,3)\|INSULATION(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BEDROCK(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|FINAL CARBONATE PRODUCT SLURRY(3,1)\|\|(WO2008/101293)\|AMMONIA(100,75)\|METHANEDIONE(100,56)\|SLURRY(100,45)\|METAL SILICATE(100,39)\|METAL SILICATE SLURRY(100,31)\|PIPELINE(100,25)\|REACTION SLURRY(100,24)\|AMMONIA WATER(100,16)\|GAS STREAM(100,10)\|FLOW PATH(100,9)\|CARBON SEQUESTRATION(100,7)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|ABSORPTION(100,2)\|CARBON SEQUESTRATION(100,2)\|METAL SILICATE ROCK(100,2)\|METAL SILICATE ROCK SLURRY(100,2)\|AMMONIA ABSORPTION(100,1)\|FLOW PATH PROVISION(100,1)\|METHANEDIONE SEQUESTRATION(88,15)\|MAGNESIUM RICH SILICATE(74,9)\|AMMONIATED SLURRY(68,5)\|EVAPORATOR(55,6)\|METAL CARBONATE(54,11)\|REACTOR(47,22)\|LIQUID PRESSURIZATION(45,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(44,1)\|REACTION ENHANCEMENT(43,4)\|AMMONIA ABSORPTION CHAMBER(38,6)\|CHILLED SLURRY(32,3)\|AMMONIA ABSORPTION CHILLER(29,2)\|AMMONIA RECOVERY VESSEL(28,14)\|PYROXENE SILICATE METAL(27,2)\|OLIVINE(23,7)\|EVAPORATOR CHAMBER(23,6)\|UNDERGROUND CHAMBER(18,8)\|RESIDUAL AMMONIA SCRUBBER(18,4)\|OVERLAND AMMONIA PIPELINE(18,2)\|RECIRCULATION(18,2)\|METAL CARBONATE PRODUCT(15,4)\|CHILLED AMMONIA WATER(15,3)\|METHANEDIONE PERMANENT SEQUESTRATION(15,1)\|CENT METHANEDIONE(14,2)\|CHAMBER PRODUCT(14,2)\|ABSORBENT SLURRY DELUGING SPRAY(14,1)\|MINERAL CARBONATION(13,3)\|PRODUCING CHAMBER(13,2)\|RESIDUAL METHANEDIONE SCRUBBER(13,1)\|AMMONIA BUBBLE(12,3)\|CO2 ABSORBER(12,3)\|HUNTER VALLEY(12,2)\|METHANEDIONE SINK(12,2)\|TARGET METAL(12,2)\|FLUE GAS(11,33)\|POWER STATION(11,21)\|RETURN PIPELINE(11,5)\|INSOLUBLE CARBONATE(11,3)\|MOLL CO2(11,3)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|UNDERGROUND REACTOR(11,2)\|CARBONATED SILICATE SLURRY(11,1)\|METHANEDIONE TONNE(11,1)\|METHANEDIONE CONTENT(10,2)\|BLACK COAL MWE(10,1)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|FINAL EMPLACEMENT REHABILITATION(10,1)\|FIROM HOT SLURRY RISING(10,1)\|INCOMING REACTANT PIPELINE(10,1)\|METHANEDIONE SCRUBBING CHAMBER(10,1)\|SILICATE SLURRY CIRCULATION(10,1)\|RAW FLUE GAS(9,6)\|AMMONIA LOSS(9,3)\|CARBONATION REACTION(9,2)\|EVAPORATOR VESSEL(9,2)\|FIRED ELECTRICITY GENERATION PLANT(9,2)\|AMMONIA TONNE(9,1)\|BICARBONATE ISIH4HCO(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|FIN FAN COOLER(9,1)\|INCOMING SILICATE SLURRY(9,1)\|INSOLUBLE MAGNESIA(9,1)\|MAXIMIZE REGENERATION(9,1)\|METHANEDIONE ABSORPTION ZONE(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OVERLAND PIPELINE(9,1)\|REACTED SLURRY RISING(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(9,1)\|STACKED SUBCHAMBER(9,1)\|FLUE GAS FILTER(8,5)\|POWER STATION FLUE GAS(8,5)\|REACTION SOLUTION(8,5)\|CARBON DIOXIDE(8,3)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|SLURRY FEED(7,2)\|ABSORBER AQ(7,1)\|AMMONIA STRIPPING(7,1)\|EMPLACEMENT SITE(7,1)\|FIRED BOILER(7,1)\|HARMFUL METHANEDIONE GAS(7,1)\|LJUNGSTROM ROTARY(7,1)\|PERMANENT EMPLACEMENT(7,1)\|PRESSURIZED AMMONIA PASS(7,1)\|RAW REACTIVE SLURRY(7,1)\|REDUCING METHANEDIONE EMISSION(7,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(7,1)\|POWER STATION SITE(6,7)\|CONDENSATION(6,3)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA MILLION(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBONATE MINERAL(6,1)\|CONCENTRATED AMMONIA(6,1)\|CONCENTRIC PIPE(6,1)\|FINAL PERMANENT REPOSITORY(6,1)\|GAS REMNANT(6,1)\|GEHO PUMP(6,1)\|INORGANIC COMPONENT(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|NATURAL SILICATE(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRETREATMENT EXTENT(6,1)\|PYROXENE RICH MINERAL(6,1)\|RAW SLURRY(6,1)\|REACTED SLURRY RISE(6,1)\|RECOVERED AMMONIA(6,1)\|RESIDUAL VAPOR(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE CONVERSION(6,1)\|SLURRY REACTION(6,1)\|TRANSPORTING ORE(6,1)\|PRESSURE EXCHANGE(5,11)\|FINAL PRODUCT SLURRY(5,4)\|00O T(5,2)\|ADJACENT FLOW PATH(5,2)\|AGITATION(5,2)\|BOTTOM ASH PULVERIZATION(5,2)\|DOLOMITE(5,2)\|LIMESTONE(5,2)\|MG3SI2O(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AMMONIA SALT(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|HOT PRODUCT PIPELINE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|METHANEDIONE SOURCE(5,1)\|OXIDE REACTION(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|VAPORIZED AMMONIA FLOW(5,1)\|WT SLURRY(5,1)\|REACTION CHAMBER(4,4)\|METAL SILICATE SOLUTION(4,3)\|POWER STATION FLY ASH(4,3)\|SOX(4,3)\|STEAM(4,3)\|INSULATION(4,2)\|AIR PREHEATING(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SOLUTION(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CO2ZGWH(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|\|(JP5345954)\|METHANEDIONE(100,72)\|GAS STREAM(100,15)\|METHANEDIONE ISOLATION(100,12)\|ISOLATION(100,6)\|METHANEDIONE ISOLATION(100,6)\|METHANEDIONE REACTION(89,6)\|AMMONIATION SLURRY(78,2)\|METAL SILICATE SLURRY(71,38)\|REACTION SLURRY(65,27)\|SOCIAL CIRCUMSTANCE(64,1)\|METAL SILICATE(62,40)\|MAGNESIUM CONTENT SILICATE(52,3)\|SILICATE SLURRY(49,26)\|REACTOR(48,31)\|CONTRACTION METHANEDIONE(45,1)\|PIPELINE(43,38)\|COLD SLURRY(39,1)\|AMMONIA(37,71)\|DISPERSED METAL SILICATE(37,1)\|AMMONIA ABSORPTION RECOVERY CONTAINER(36,1)\|UNDERGROUND CHAMBER(33,4)\|AMMONISED SLURRY(33,2)\|METAL CARBONATE(31,11)\|SUBTERRANEAN INSTALLED CHAMBER(31,1)\|METHANEDIONE STREAM(30,2)\|PIPELINE SPEED(29,1)\|RECOVERY SLURRY REACTION(29,1)\|PRESSURIZED RECOVERY CONTAINER(28,2)\|NATURAL ABSORPTION(27,2)\|COLLECTION CONTAINER(27,1)\|METER(27,1)\|PRESSURIZED AMMONIA(25,3)\|SLURRY(23,35)\|AMMONIA ABSORPTION CHAMBER(23,7)\|FLOW PATH(22,10)\|AMMONIA LOSS(22,4)\|AMMONIA WATER(21,21)\|EVAPORATOR CHAMBER(20,7)\|COOLED SLURRY(19,4)\|METAL SILICATE ROCK SLURRY(19,2)\|FINAL FLUE GAS(19,1)\|REACTOR CONTROL(18,2)\|AMMONIA RECOVERY VESSEL(17,7)\|MINING STATION(16,9)\|FLOW CHANNEL(16,2)\|SLIP(16,1)\|RESIDUAL AMMONIA SCRUBBER(15,4)\|METHANEDIONE ISOLATING(15,3)\|REACTOR PRESSURE(15,1)\|CORUNDUITE(14,4)\|RECYCLING(14,2)\|FLUE GAS(13,35)\|LATE PARAGRAPH(13,4)\|METAL CARBONATE PRODUCT(13,4)\|AMMONIA BUBBLE(11,3)\|MINERAL CARBONATION(11,3)\|ABSORBED METHANEDIONE TON(11,1)\|INSOLUBLE MAGNESIA PRECIPITATION(11,1)\|RESIDUAL METHANEDIONE SCRUBBER(11,1)\|HEAT EXCHANGER(10,26)\|RETURN PIPELINE(10,5)\|CO2 ABSORBER(10,3)\|PULVERIZED COAL BURNING(10,1)\|POWER PLANT(9,31)\|COOLED AMMONIA WATER(9,4)\|HOT SILICATE SLURRY(9,2)\|HUNTER VALLEY(9,2)\|INCOMING REACTIVE SLURRY(9,2)\|UNDERGROUND REACTOR(9,2)\|INCOMING REACTANT PIPELINE(9,1)\|METHANEDIONE ABSORBER(9,1)\|METHANEDIONE SCRUBBING CHAMBER(9,1)\|SCRUBBING CHAMBER HEADSPACE(9,1)\|SERPENTINE MINING SITE(9,1)\|SILICATE SLURRY CIRCULATION(9,1)\|SPRAYED ABSORBENT SLURRY(9,1)\|STACKED SUBCHAMBER(9,1)\|REACTION SOLUTION(7,5)\|UNTREATED FLUE GAS(7,5)\|POWER PLANT FLUE GAS(7,4)\|EVAPORATOR CONTAINER(7,2)\|AMMONIATED SLURRY(7,1)\|CRUSHED LIMESTONE(7,1)\|FEEDSTOCK COAL(7,1)\|INCOMING SILICATE SLURRY(7,1)\|METHANEDIONE ABSORPTION ZONE(7,1)\|METHANEDIONE EMISSION(7,1)\|METHANEDIONE PROMOTING REACTION(7,1)\|MINING SITE VICINITY(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(7,1)\|SILICATE SLURRY COOLING(7,1)\|SUBTERRANEAN CHAMBER REACTOR(7,1)\|SUBTERRANEAN PIPELINE(7,1)\|SUPERBITTER ROCK(7,1)\|UNTREATED REACTIVE SLURRY(7,1)\|HEAT TRANSFER(6,2)\|HOT SLURRY(6,2)\|MAGNESIUM ION(6,2)\|PUMPING ENERGY(6,2)\|SLURRY FEED(6,2)\|AMMONIA COLLECTION VESSEL(6,1)\|AMMONIA VAPORIZATION(6,1)\|BURNING BOILER(6,1)\|CARBON ISOLATION NONLIMITING(6,1)\|COLD SILICATE SLURRY(6,1)\|COOLED SILICATE SLURRY(6,1)\|DEINKED ASH(6,1)\|DOLOMITE LIME(6,1)\|ECONOMIC STANDPOINT(6,1)\|FAN CONCENTRIC PIPE(6,1)\|GROUND AMMONIA PIPELINE(6,1)\|LJUNGSTROM ROTARY(6,1)\|METHANEDIONE CONVERSION(6,1)\|METHANEDIONE DISCHARGE(6,1)\|METHANEDIONE SEPARATION(6,1)\|MILLED SLURRY(6,1)\|RESIDUAL AMMONIA COLLECTOR(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|STEAM INJECTION(6,1)\|UNTREATED SLURRY(6,1)\|FINAL PRODUCT SLURRY(5,5)\|FLUE GAS FILTER(5,3)\|MG3SI2O(5,3)\|METHANEDIONE SOURCE(5,2)\|ALKALINE INDUSTRIAL RESIDUE(5,1)\|AMMONIA CONDENSATION(5,1)\|AMMONIA RECOVERY CONTAINER CONTENT(5,1)\|AMMONIA SLURRY(5,1)\|AMMONIA TON(5,1)\|BURNED ASH(5,1)\|BYPRODUCT SILICA(5,1)\|CARBONATE MINERAL(5,1)\|CIRCULATION NATURAL VELOCITY(5,1)\|CO2 MCO(5,1)\|COAL FUEL(5,1)\|COLLECTED AMMONIA(5,1)\|DISSOLVE TARGET(5,1)\|ELEMENTAL IRON(5,1)\|EVAPORATOR VESSEL(5,1)\|EXTRACT MAGNESIUM(5,1)\|INSOLUBLE CARBONATE SALT(5,1)\|MAGNESIA REACTION(5,1)\|METHANEDIONE CONTENT(5,1)\|MINE CAVITY(5,1)\|NATURAL DRAFT COOLING TOWER(5,1)\|NATURALLY OCCURRING SILICATE ROCK(5,1)\|PERMANENT INSULATION(5,1)\|PLANT FACILITY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTION SLURRY RISING(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|POWER PLANT FLY ASH(4,4)\|ANTIOFFICE(4,2)\|CARBAMATE(4,2)\|FINAL PLACEMENT LOCATION(4,2)\|MG2SIO(4,2)\|PARTICULATE(4,2)\|RAW FLUE GAS(4,2)\|SOUTH WALL(4,2)\|WOLLASTONITE(4,2)\|ABSORBING CHAMBER(4,1)\|ACTIVE SUBSTANCE OXIDATION(4,1)\|AMMONIA REACTION(4,1)\|AMMONIA REGENERATION RATE(4,1)\|AUDIT(4,1)\|BASELOAD MODE(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENTRAL CARBONATION REACTION(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|CONVEYANCE(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DESIRABLE SILICATE ROCK(4,1)\|DESIRED HEAT TRANSFER(4,1)\|DIFFUSED METAL SILICATE(4,1)\|DISCHARGE RECTIFICATION VESSEL(4,1)\|FIBROUS FILTER(4,1)\|FIN FAN(4,1)\|FRICTION LOSS(4,1)\|GEHO PUMP(4,1)\|HARMFUL METHANEDIONE GAS SOURCE(4,1)\|HYDROSTATIC HEAD USABLE DEPTH(4,1)\|LUMPY PRODUCT(4,1)\|MAGNESIUM RICH SILICATE(4,1)\|MAGNESIUM STABILITY(4,1)\|METHANEDIONE SEQUESTRATION(4,1)\|MILLED METAL SILICATE(4,1)\|NATURAL SILICATE(4,1)\|PERMANENT PLACEMENT(4,1)\|PIPE REACTOR(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PROMOTION(4,1)\|RADIITE SILICATE METAL(4,1)\|REACTION STEP(4,1)\|REINCREASE(4,1)\|RESIDUAL VAPOR(4,1)\|SLURRY SUPPLY(4,1)\|TRANSPORT FEW HOUR(4,1)\|TUBULAR REACTOR(4,1)\|AMBIENT TEMPERATURE(3,3)\|EXOTHERMIC REACTION(3,3)\|GWH(3,3)\|METAL SILICATE SOLUTION(3,3)\|MWE(3,3)\|ORE(3,3)\|ABSORB REMAINING MANIFEST HEAT(3,1)\|AIR PREHEATING(3,1)\|ALKALINITY(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA CONTENT(3,1)\|AMMONIA RECOVERY VESSEL TOP(3,1)\|AMMONIA REMOVAL(3,1)\|AMMONIA RICH SOLUTION(3,1)\|ANNULUS(3,1)\|BICARBONATE(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CLEAN FLUE GAS(3,1)\|COOL FILTER(3,1)\|COOLED FILTER FLUE GAS(3,1)\|\|(JP2010519027)\|AMMONIA(100,76)\|METHANEDIONE(100,71)\|METAL SILICATE(100,45)\|SLURRY(100,42)\|METAL SILICATE SLURRY(100,39)\|REACTION SLURRY(100,31)\|AMMONIA WATER(100,22)\|METHANEDIONE ISOLATION(100,14)\|GAS STREAM(100,13)\|FLOW PATH(100,8)\|ISOLATION(100,6)\|METHANEDIONE ISOLATION(100,6)\|ABSORPTION(100,4)\|METAL SILICATE ROCK(100,4)\|METAL SILICATE ROCK SLURRY(100,4)\|CARBON ISOLATION(100,3)\|AMMONIA ABSORPTION(100,2)\|METHANEDIONE REACTION(97,6)\|AMMONIATION SLURRY(71,1)\|SOCIAL CIRCUMSTANCE(65,1)\|ABSORBED METHANEDIONE(53,2)\|METAL CARBONATE(52,15)\|SILICATE SLURRY(50,27)\|REACTOR(49,30)\|SUBTERRANEAN FORMATION(46,1)\|PRESSURIZED AMMONIA(45,2)\|EVAPORATOR(44,8)\|COLD SLURRY(40,1)\|DISSOLVE TARGET(39,2)\|GAS TURBINE SUBTERRANEAN FORMATION(39,1)\|PIPELINE(37,35)\|DISPERSED METAL SILICATE(37,1)\|AMMONIA ABSORPTION RECOVERY CONTAINER(36,1)\|AMMONISED SLURRY(34,2)\|AMMONIA ABSORPTION CHAMBER(33,8)\|AMMONIA ABSORPTION CHILLER(31,1)\|CHAMBER INSTALLED UNDERGROUND(31,1)\|METHANEDIONE STREAM(30,2)\|PRESSURIZED RECOVERY CONTAINER(29,2)\|PIPELINE SPEED(29,1)\|NATURAL ABSORPTION(28,2)\|COLLECTION CONTAINER(27,1)\|METER(27,1)\|AMMONIA LOSS(23,4)\|CORUNDUITE(22,5)\|RADIITE SILICATE METAL(22,2)\|EVAPORATOR CHAMBER(20,7)\|COOLED SLURRY(19,4)\|FINAL FLUE GAS(19,1)\|AMMONIA RECOVERY VESSEL(18,7)\|REACTOR CONTROL(18,2)\|GAS TURBINE(18,1)\|MINING STATION(17,9)\|FLOW CHANNEL(17,2)\|SLIP(17,1)\|HEAT EXCHANGER(16,28)\|RESIDUAL AMMONIA SCRUBBER(16,4)\|TARGET METAL(16,4)\|REACTOR PRESSURE(16,1)\|METHANEDIONE ISOLATING(15,3)\|FLUE GAS(14,36)\|RECYCLING(14,2)\|LATE PARAGRAPH(13,4)\|METAL CARBONATE PRODUCT(13,4)\|POWER PLANT(12,33)\|HIGH MAGNESIUM CONTENT SILICATE(12,10)\|PRODUCING CHAMBER(12,2)\|AMMONIA BUBBLE(11,3)\|MINERAL CARBONATION(11,3)\|AMMONIATED SLURRY(11,2)\|ABSORBED METHANEDIONE TON(11,1)\|INSOLUBLE MAGNESIA PRECIPITATION(11,1)\|RESIDUAL METHANEDIONE SCRUBBER(11,1)\|RETURN PIPELINE(10,5)\|CO2 ABSORBER(10,3)\|PULVERIZED COAL BURNING(10,1)\|COOLED AMMONIA WATER(9,4)\|HOT SILICATE SLURRY(9,2)\|HUNTER VALLEY(9,2)\|INCOMING REACTIVE SLURRY(9,2)\|UNDERGROUND REACTOR(9,2)\|INCOMING REACTANT PIPELINE(9,1)\|METHANEDIONE ABSORBER(9,1)\|METHANEDIONE SCRUBBING CHAMBER(9,1)\|SCRUBBING CHAMBER HEADSPACE(9,1)\|SERPENTINE MINING SITE(9,1)\|SILICATE SLURRY CIRCULATION(9,1)\|SPRAYED ABSORBENT SLURRY(9,1)\|STACKED SUBCHAMBER(9,1)\|POWER PLANT FLUE GAS(8,4)\|EVAPORATOR CONTAINER(8,2)\|AMMONIA ABSORPTION COOLER(8,1)\|CRUSHED LIMESTONE(8,1)\|FEEDSTOCK COAL(8,1)\|INCOMING SILICATE SLURRY(8,1)\|METHANEDIONE ABSORPTION ZONE(8,1)\|METHANEDIONE EMISSION(8,1)\|MINING SITE VICINITY(8,1)\|MULTISTAGE BARREL PUMP(8,1)\|RESIDUAL AMMONIA ABSORBER(8,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(8,1)\|SILICATE SLURRY COOLING(8,1)\|SUBTERRANEAN CHAMBER REACTOR(8,1)\|SUBTERRANEAN PIPELINE(8,1)\|SUPERBITTER ROCK(8,1)\|UNTREATED REACTIVE SLURRY(8,1)\|REACTION SOLUTION(7,5)\|UNTREATED FLUE GAS(7,5)\|UNDERGROUND CHAMBER(7,2)\|HEAT TRANSFER(6,2)\|HOT SLURRY(6,2)\|MAGNESIUM ION(6,2)\|PUMPING ENERGY(6,2)\|SLURRY FEED(6,2)\|AMMONIA COLLECTION VESSEL(6,1)\|AMMONIA VAPORIZATION(6,1)\|BURNING BOILER(6,1)\|CARBON ISOLATION NONLIMITING(6,1)\|COLD SILICATE SLURRY(6,1)\|COOLED SILICATE SLURRY(6,1)\|DEINKED ASH(6,1)\|DOLOMITE LIME(6,1)\|ECONOMIC STANDPOINT(6,1)\|GROUND AMMONIA PIPELINE(6,1)\|LJUNGSTROM ROTARY(6,1)\|METHANEDIONE CONVERSION(6,1)\|METHANEDIONE DISCHARGE(6,1)\|METHANEDIONE SEPARATION(6,1)\|MILLED SLURRY(6,1)\|RESIDUAL AMMONIA COLLECTOR(6,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(6,1)\|STEAM INJECTION(6,1)\|UNTREATED SLURRY(6,1)\|FINAL PRODUCT SLURRY(5,5)\|FLUE GAS FILTER(5,3)\|MG3SI2O(5,3)\|CHAMBER PRODUCT FLOW PATH(5,2)\|METHANEDIONE SOURCE(5,2)\|ALKALINE INDUSTRIAL RESIDUE(5,1)\|AMMONIA CONDENSATION(5,1)\|AMMONIA RECOVERY CONTAINER CONTENT(5,1)\|AMMONIA TON(5,1)\|BURNED ASH(5,1)\|BYPRODUCT SILICA(5,1)\|CARBONATE MINERAL(5,1)\|CIRCULATION NATURAL VELOCITY(5,1)\|CO2 MCO(5,1)\|COAL FUEL(5,1)\|COLLECTED AMMONIA(5,1)\|CONCENTRIC PIPE(5,1)\|ELEMENTAL IRON(5,1)\|EVAPORATOR VESSEL(5,1)\|EXTRACT MAGNESIUM(5,1)\|INSOLUBLE CARBONATE SALT(5,1)\|MAGNESIA REACTION(5,1)\|METHANEDIONE CONTENT(5,1)\|MINE CAVITY(5,1)\|NATURAL DRAFT COOLING TOWER(5,1)\|NATURALLY OCCURRING SILICATE ROCK(5,1)\|PERMANENT INSULATION(5,1)\|PLANT FACILITY(5,1)\|REACTED SLURRY RISE(5,1)\|REACTION SLURRY RISING(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|POWER PLANT FLY ASH(4,4)\|REACTION CHAMBER(4,4)\|CARBAMATE(4,2)\|FINAL PLACEMENT LOCATION(4,2)\|MG2SIO(4,2)\|PARTICULATE(4,2)\|RAW FLUE GAS(4,2)\|SOUTH WALL(4,2)\|WOLLASTONITE(4,2)\|ABSORBING CHAMBER(4,1)\|ACTIVE SUBSTANCE OXIDATION(4,1)\|AMMONIA REACTION(4,1)\|AMMONIA REGENERATION RATE(4,1)\|AUDIT(4,1)\|BASELOAD MODE(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENTRAL CARBONATION REACTION(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|CONVEYANCE(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DESIRABLE SILICATE ROCK(4,1)\|DESIRED HEAT TRANSFER(4,1)\|DISCHARGE RECTIFICATION VESSEL(4,1)\|FIBROUS FILTER(4,1)\|FIN FAN(4,1)\|FRICTION LOSS(4,1)\|GEHO PUMP(4,1)\|HARMFUL METHANEDIONE GAS SOURCE(4,1)\|HYDROSTATIC HEAD USABLE DEPTH(4,1)\|LUMPY PRODUCT(4,1)\|MAGNESIUM RICH SILICATE(4,1)\|MAGNESIUM STABILITY(4,1)\|METHANEDIONE SEQUESTRATION(4,1)\|MILLED METAL SILICATE(4,1)\|NATURAL SILICATE(4,1)\|PERMANENT PLACEMENT(4,1)\|PIPE REACTOR(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|REACTION STEP(4,1)\|REINCREASE(4,1)\|RESIDUAL VAPOR(4,1)\|SLURRY SUPPLY(4,1)\|TRANSPORT FEW HOUR(4,1)\|TUBULAR REACTOR(4,1)\|AMBIENT TEMPERATURE(3,3)\|EXOTHERMIC REACTION(3,3)\|GWH(3,3)\|METAL SILICATE SOLUTION(3,3)\|MWE(3,3)\|ORE(3,3)\|ABSORB REMAINING MANIFEST HEAT(3,1)\|AIR PREHEATING(3,1)\|ALKALINITY(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA CONTENT(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA RECOVERY VESSEL TOP(3,1)\|AMMONIA REMOVAL(3,1)\|AMMONIA RICH SOLUTION(3,1)\|ANNULUS(3,1)\|BICARBONATE(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CHESHUNT MIXTURE COMPOUND(3,1)\|CLEAN FLUE GAS(3,1)\|COOL FILTER(3,1)\|\|(CN101641145)\|CARBON DIOXIDE(100,114)\|SLURRY(100,42)\|REACTION SLURRY(100,32)\|CARBON DIOXIDE SEQUESTRATION(100,18)\|GAS STREAM(100,7)\|SEQUESTERING CARBON DIOXIDE(100,3)\|METAL SILICATE SLURRY(88,36)\|AMMONIA ABSORPTION RECOVERY VESSEL(79,1)\|METAL SILICATE(72,39)\|AMMONIATED SLURRY(71,5)\|CHAMBER REACTOR(71,3)\|ABSORPTION RECOVERY VESSEL(68,1)\|SUBTERRANEAN REACTOR(66,1)\|MAGNESIUM RICH SILICATE(54,7)\|REACTION SLURRY RISING(51,1)\|METAL CARBONATE(49,14)\|PERMANENT INSULATION(49,1)\|AMMONIA(48,63)\|METAL SILICATE ROCK(45,4)\|NATURALLY OCCURRING SINK(40,1)\|REACTOR(39,21)\|PHOTOSYNTHESIS(36,1)\|CHILLED SLURRY(35,2)\|PIPELINE REACTOR(33,4)\|CARBONATE PRODUCT(32,4)\|AMMONIA GAS BUBBLE(32,1)\|AMMONIA RECOVERY VESSEL(30,14)\|AMMONIA ABSORPTION CHILLER(30,2)\|AMMONIA LOSS(29,3)\|BIOMASS(28,1)\|EVAPORATION CHAMBER(28,1)\|SEPARATING CARBON DIOXIDE(27,1)\|CHAMBER PRODUCT(26,2)\|AMMONIA WATER(25,20)\|ELECTRICITY DEMAND(25,1)\|RAW FLUE GAS(21,6)\|METAL CARBONATE PRODUCT(21,4)\|REMOVING CARBON DIOXIDE(21,2)\|HEAT EXCHANGER(20,25)\|CARBON CAPTURE(20,1)\|RESIDUAL AMMONIA SCRUBBER(19,4)\|REACTION ENHANCEMENT(19,2)\|COLLECTION POINT(19,1)\|CHILLED AMMONIA WATER(17,2)\|PRESSURIZED LIQUID AMMONIA(17,2)\|BULK DENSITY(17,1)\|AMMONIA GAS(16,1)\|JACKETED ABOVEGROUND PIPELINE(16,1)\|FLUE GAS(15,33)\|AMMONIA ABSORPTION CHAMBER(15,5)\|MINERAL CARBONATION(14,3)\|ABSORBENT SLURRY DELUGE SPRAY(14,1)\|CARBON DIOXIDE COLLECTION POINT(14,1)\|SOUTH HUNTER VALLEY(14,1)\|POWER PLANT(13,31)\|INSOLUBLE CARBONATE(13,4)\|PRODUCING CHAMBER(13,3)\|AMMONIA ABSORPTION(13,2)\|CARBON DIOXIDE REACTION(13,2)\|ONSHORE AMMONIA PIPELINE(13,1)\|EVAPORATOR CHAMBER(12,5)\|WASHING CHAMBER(12,5)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|STATIC HEAD(10,3)\|AMMONIA BUBBLE(10,2)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|PRETREATMENT ABOVETHE EXTENT(10,1)\|RECYCLED SILICATE SLURRY(10,1)\|SCRUBBING CHAMBER HEADSPACE(10,1)\|STACKED SUBCOMPARTMENT(10,1)\|POWER PLANT FLUE GAS(9,5)\|REACTION SOLUTION(9,5)\|EVAPORATOR VESSEL(9,2)\|RECOVERING AMMONIA(9,2)\|CARBON DIOXIDEON CAPTURE(9,1)\|INCOMING SILICATE SLURRY(9,1)\|LOW NOX BURNER(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OLIVINE STONE(9,1)\|ONSHORE PIPELINE(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|AMMONIUM SALT(8,4)\|DOLOMITE(8,4)\|FLUE GAS FILTER(8,4)\|GAS MIXTURE(8,2)\|COLD SILICATE SLURRY(8,1)\|CRUDE REACTION SLURRY(8,1)\|DEINKING ASH(8,1)\|DELUGING SPRAY(8,1)\|DENSER SLURRY(8,1)\|LJUNGSTROM ROTARY(8,1)\|MAXIMIZE REGENERATION(8,1)\|OLIVINE RICH(8,1)\|POWDERED LIMESTONE(8,1)\|RECYCLED SCRUBBING MEDIUM(8,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(8,1)\|SERPENTINE STONE(8,1)\|SLURRY CIRCULATION(8,1)\|ULTIMATE LOCATION REHABILITATION(8,1)\|UNDERGROUND REACTOR(8,1)\|CARBON DIOXIDE TON(7,3)\|CARBON SEQUESTRATION(7,3)\|PUMPING ENERGY(7,2)\|POWER PLANT SITE(6,6)\|CONDENSATION(6,3)\|ALKALI INDUSTRY RESIDUE(6,1)\|AMMONIA FLASH(6,1)\|AMMONIA MILLION(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(6,1)\|CARBONATE MINERAL(6,1)\|COAL DUST BOILER(6,1)\|COAL FUEL(6,1)\|CONCENTRATED AMMONIA(6,1)\|CORE CARBONATION REACTION(6,1)\|DISSOLVE TARGET(6,1)\|FIN FAN COOLER(6,1)\|FROZEN METAL SILICATE SLURRY(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INSOLUBLE MAGNESIUM HYDROXIDE PRECIPITATION(6,1)\|MAGNESIUM PRECIPITATE(6,1)\|MINE VOID(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PUMPING CAPABILITY(6,1)\|PYROXENE RICH MINERAL(6,1)\|PYROXENE SILICATE METAL(6,1)\|RAW COAL(6,1)\|RAW SLURRY(6,1)\|REACTOR CHOICE(6,1)\|RESIDUAL STEAM(6,1)\|SCRUBBING MEDIA(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE SLURRY DENSITY(6,1)\|SILICATE SLURRY FLOW CARBONATION(6,1)\|TRANSPORTING ORE(6,1)\|CARBON DIOXIDE SEQUESTRATION(5,4)\|FINAL PRODUCT SLURRY(5,4)\|MAGNESIUM CARBONATE(5,4)\|POWER PLANT FLY ASH(5,4)\|PRESSURE EXCHANGE(5,4)\|ABSORBER DETAIL(5,2)\|ADJACENT FLOW PATH(5,2)\|CARBON DIOXIDE EMISSION(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AMMONIA RICH SOLUTION(5,1)\|AMMONIA TON HOUR(5,1)\|CARBONATE SILICATE SLURRY(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|CONCENTRIC TUBE(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|FINAL COLD SLURRY FEED(5,1)\|FLASH RECTIFIER VESSEL(5,1)\|FRICTION LOSS(5,1)\|GRADUAL DECREASE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|MILLION KILOWATT HOUR(5,1)\|NATURAL DRAFT COOLING TOWER(5,1)\|PARTICLE CLEANING(5,1)\|PERMANENT PLACEMENT(5,1)\|PREPROCESSING(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|REJUVENATION(5,1)\|SLURRY COOLING(5,1)\|STEAM TON HOUR(5,1)\|STRATEGIC LOCATION(5,1)\|SUPPLEMENTAL HEATING(5,1)\|TUBE BUNDLE(5,1)\|WET GRINDING(5,1)\|JET PUMP(4,4)\|AMBIENT TEMPERATURE(4,3)\|BLACK COAL(4,3)\|EXOTHERMIC REACTION(4,3)\|HYDROSTATIC HEAD(4,3)\|SHELL(4,2)\|SINGLE INTEGRATED(4,2)\|ABSORB REMAINING SENSIBLE HEAT(4,1)\|AIR PREHEATING(4,1)\|ALKALI RICH METAL SILICATE(4,1)\|AMMONIA ABSORBER(4,1)\|AMMONIA CONTENT(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA RECOVERY VESSEL BOTTOM(4,1)\|AMMONIA RECOVERY VESSEL TOP(4,1)\|AMMONIASHOULD(4,1)\|AMMONIUM CARBONATE COMPOUND(4,1)\|ARRIVAL PRESSURE(4,1)\|BASEMENT DESIGN(4,1)\|BEDROCK(4,1)\|BICARBONATE(4,1)\|BOTTOM ASH PULVERIZATION(4,1)\|BULK PRODUCT(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CARBON DIOXIDE ABSORPTION ZONE(4,1)\|CARBON DIOXIDE SCRUBBER CHAMBER(4,1)\|CARBON DIOXIDE SCRUBBING MEDIUM(4,1)\|CARBON DIOXIDE SINK(4,1)\|CHILLED SOLUTION(4,1)\|CLEAN FLUE GAS(4,1)\|COAGULATION(4,1)\|COMMINUTION(4,1)\|CONDUCTING CARBON DIOXIDE(4,1)\|CONSTRUCTED STORAGE COMPARTMENT(4,1)\|COOLER GAS(4,1)\|DESTRUCTION(4,1)\|DOSING(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|ENERGY BURDEN(4,1)\|EXCESS HEAT(4,1)\|\|(CN101641145)\|CARBON DIOXIDE(100,117)\|AMMONIA(100,66)\|METAL SILICATE(100,45)\|SLURRY(100,43)\|METAL SILICATE SLURRY(100,36)\|REACTION SLURRY(100,32)\|AMMONIA WATER(100,20)\|CARBON DIOXIDE SEQUESTRATION(100,18)\|PIPELINE(100,15)\|FLOW PATH(100,11)\|CARBON SEQUESTRATION(100,9)\|GAS STREAM(100,7)\|ABSORPTION(100,5)\|CARBON DIOXIDE SEQUESTRATION(100,5)\|SEQUESTRATION(100,5)\|METAL SILICATE ROCK(100,4)\|METAL SILICATE ROCK SLURRY(100,4)\|CARBON SEQUESTRATION(100,3)\|SEQUESTERING CARBON DIOXIDE(100,3)\|AMMONIA ABSORPTION(100,2)\|MAGNESIUM RICH SILICATE(77,9)\|AMMONIATED SLURRY(68,5)\|SUBTERRANEAN REACTOR(63,1)\|METAL CARBONATE(54,15)\|REACTOR(53,26)\|EVAPORATOR(52,8)\|REACTION SLURRY RISING(49,1)\|PERMANENT INSULATION(46,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(43,1)\|NATURALLY OCCURRING SINK(38,1)\|AMMONIA ABSORPTION CHAMBER(37,7)\|FROZEN SLURRY(37,1)\|PHOTOSYNTHESIS(34,1)\|AMMONIA GAS BUBBLE(31,1)\|LIQUID PRESSURIZATION(30,2)\|AMMONIA RECOVERY VESSEL(29,14)\|AMMONIA ABSORPTION CHILLER(29,2)\|AMMONIUM SALT(27,5)\|AMMONIA LOSS(27,3)\|PYROXENE SILICATE METAL(27,2)\|BIOMASS(27,1)\|SEPARATING CARBON DIOXIDE(25,1)\|ELECTRICITY DEMAND(24,1)\|EVAPORATOR CHAMBER(23,6)\|CARBON DIOXIDE REACTION(21,2)\|RAW FLUE GAS(20,6)\|REMOVING CARBON DIOXIDE(20,2)\|CARBON CAPTURE(19,1)\|RESIDUAL AMMONIA SCRUBBER(18,4)\|TARGET METAL(18,4)\|REACTION ENHANCEMENT(18,2)\|COLLECTION POINT(18,1)\|FLUE GAS(16,34)\|CHILLED AMMONIA WATER(16,2)\|BULK DENSITY(16,1)\|POWER PLANT(15,33)\|METAL CARBONATE PRODUCT(15,4)\|AMMONIA GAS(15,1)\|JACKETED ABOVEGROUND PIPELINE(15,1)\|CHAMBER PRODUCT(14,2)\|ABSORBENT SLURRY DELUGE SPRAY(14,1)\|CARBON DIOXIDE COLLECTION POINT(14,1)\|SOUTH HUNTER VALLEY(14,1)\|MINERAL CARBONATION(13,3)\|PIPELINE REACTOR(13,3)\|INSOLUBLE CARBONATE(12,4)\|PRODUCING CHAMBER(12,3)\|ONSHORE AMMONIA PIPELINE(12,1)\|WASHING CHAMBER(11,5)\|AMMONIA BUBBLE(10,2)\|HOT SILICATE SLURRY(10,2)\|INCOMING REACTIVE SLURRY(10,2)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|RECYCLED SILICATE SLURRY(10,1)\|SCRUBBING CHAMBER HEADSPACE(10,1)\|STACKED SUBCOMPARTMENT(10,1)\|STATIC HEAD(9,3)\|EVAPORATOR VESSEL(9,2)\|RECOVERING AMMONIA(9,2)\|INCOMING SILICATE SLURRY(9,1)\|LOW NOX BURNER(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OLIVINE STONE(9,1)\|ONSHORE PIPELINE(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|POWER PLANT FLUE GAS(8,5)\|REACTION SOLUTION(8,5)\|GAS MIXTURE(8,2)\|DOLOMITE(7,4)\|FLUE GAS FILTER(7,4)\|PUMPING ENERGY(7,2)\|CHILLED SLURRY(7,1)\|COLD SILICATE SLURRY(7,1)\|CRUDE REACTION SLURRY(7,1)\|DEINKING ASH(7,1)\|DELUGING SPRAY(7,1)\|DENSER SLURRY(7,1)\|LJUNGSTROM ROTARY(7,1)\|MAXIMIZE REGENERATION(7,1)\|OLIVINE RICH(7,1)\|POWDERED LIMESTONE(7,1)\|RECYCLED SCRUBBING MEDIUM(7,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(7,1)\|SERPENTINE STONE(7,1)\|SLURRY CIRCULATION(7,1)\|ULTIMATE LOCATION REHABILITATION(7,1)\|UNDERGROUND REACTOR(7,1)\|POWER PLANT SITE(6,6)\|CARBON DIOXIDE TON(6,3)\|ALKALI INDUSTRY RESIDUE(6,1)\|AMMONIA FLASH(6,1)\|AMMONIA MILLION(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(6,1)\|CARBONATE MINERAL(6,1)\|COAL DUST BOILER(6,1)\|COAL FUEL(6,1)\|CONCENTRATED AMMONIA(6,1)\|CORE CARBONATION REACTION(6,1)\|DISSOLVE TARGET(6,1)\|FIN FAN COOLER(6,1)\|FROZEN METAL SILICATE SLURRY(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INSOLUBLE MAGNESIUM HYDROXIDE PRECIPITATION(6,1)\|MAGNESIUM PRECIPITATE(6,1)\|MINE VOID(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PUMPING CAPABILITY(6,1)\|PYROXENE RICH MINERAL(6,1)\|RAW COAL(6,1)\|RAW SLURRY(6,1)\|REACTOR CHOICE(6,1)\|RESIDUAL STEAM(6,1)\|SCRUBBING MEDIA(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE SLURRY DENSITY(6,1)\|SILICATE SLURRY FLOW CARBONATION(6,1)\|TRANSPORTING ORE(6,1)\|FINAL PRODUCT SLURRY(5,4)\|MAGNESIUM CARBONATE(5,4)\|POWER PLANT FLY ASH(5,4)\|PRESSURE EXCHANGE(5,4)\|CONDENSATION(5,3)\|ABSORBER DETAIL(5,2)\|ADJACENT FLOW PATH(5,2)\|CARBON DIOXIDE EMISSION(5,2)\|PRETREATMENT(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AMMONIA RICH SOLUTION(5,1)\|AMMONIA TON HOUR(5,1)\|CARBONATE SILICATE SLURRY(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|CONCENTRIC TUBE(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|FINAL COLD SLURRY FEED(5,1)\|FLASH RECTIFIER VESSEL(5,1)\|FRICTION LOSS(5,1)\|GRADUAL DECREASE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|MILLION KILOWATT HOUR(5,1)\|NATURAL DRAFT COOLING TOWER(5,1)\|PARTICLE CLEANING(5,1)\|PERMANENT PLACEMENT(5,1)\|PREPROCESSING(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|REJUVENATION(5,1)\|SLURRY COOLING(5,1)\|STEAM TON HOUR(5,1)\|STRATEGIC LOCATION(5,1)\|SUPPLEMENTAL HEATING(5,1)\|TUBE BUNDLE(5,1)\|WET GRINDING(5,1)\|JET PUMP(4,4)\|AMBIENT TEMPERATURE(4,3)\|BLACK COAL(4,3)\|EXOTHERMIC REACTION(4,3)\|HYDROSTATIC HEAD(4,3)\|SHELL(4,2)\|SINGLE INTEGRATED(4,2)\|ABSORB REMAINING SENSIBLE HEAT(3,1)\|AIR PREHEATING(3,1)\|ALKALI RICH METAL SILICATE(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA CONTENT(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA RECOVERY VESSEL BOTTOM(3,1)\|AMMONIA RECOVERY VESSEL TOP(3,1)\|AMMONIUM CARBONATE COMPOUND(3,1)\|ARRIVAL PRESSURE(3,1)\|BASEMENT DESIGN(3,1)\|BEDROCK(3,1)\|BOTTOM ASH PULVERIZATION(3,1)\|BULK PRODUCT(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CARBON DIOXIDE ABSORPTION ZONE(3,1)\|CARBON DIOXIDE CAPTURE(3,1)\|CARBON DIOXIDE SCRUBBER CHAMBER(3,1)\|CARBON DIOXIDE SCRUBBING MEDIUM(3,1)\|CARBON DIOXIDE SINK(3,1)\|CARBONHYDROGEN ACID SALT(3,1)\|CHILLED SOLUTION(3,1)\|CLEAN FLUE GAS(3,1)\|COAGULATION(3,1)\|COMMINUTION(3,1)\|CONDUCTING CARBON DIOXIDE(3,1)\|CONSTRUCTED STORAGE COMPARTMENT(3,1)\|COOLER GAS(3,1)\|DESTRUCTION(3,1)\|DOSING(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|\|(IN293376)\|METHANEDIONE(100,57)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,11)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|REACTION SLURRY(92,25)\|METAL SILICATE SLURRY(81,30)\|METAL SILICATE(74,35)\|AMMONIATED SLURRY(73,5)\|REACTOR(53,24)\|PRESSURIZED AMMONIA(50,1)\|ABSORBED METHANEDIONE(47,1)\|AMMONIA ABSORPTION RECOVERY VESSEL(47,1)\|AMMONIA(44,73)\|METAL SILICATE ROCK(43,2)\|METAL CARBONATE(39,9)\|REACTION ENHANCEMENT(35,5)\|CHILLED SLURRY(34,3)\|AMMONIA ABSORPTION CHILLER(31,2)\|AMMONIA RECOVERY VESSEL(30,14)\|FLOW PATH(30,11)\|UNDERGROUND CHAMBER(30,10)\|EVAPORATION CHAMBER(29,1)\|SLURRY(28,41)\|MAGNESIUM SILICATE(25,2)\|AMMONIA WATER(24,16)\|RESIDUAL AMMONIA SCRUBBER(19,4)\|OVERLAND AMMONIA PIPELINE(19,2)\|METAL CARBONATE PRODUCT(16,4)\|CHILLED AMMONIA WATER(16,3)\|LAGGED ABOVEGROUND PIPELINE(16,1)\|METHANEDIONE PERMANENT SEQUESTRATION(16,1)\|RESULTANT AMMONIA WATER(16,1)\|ABSORBENT SLURRY DELUGING SPRAY(15,1)\|MINERAL CARBONATION(14,3)\|AMMONIA ABSORPTION CHAMBER(13,4)\|AMMONIA BUBBLE(13,3)\|HUNTER VALLEY(13,2)\|METHANEDIONE CAPTURE(13,2)\|METHANEDIONE SINK(13,2)\|RESIDUAL METHANEDIONE SCRUBBER(13,1)\|EVAPORATOR CHAMBER(12,5)\|RETURN PIPELINE(12,5)\|CO2 ABSORBER(12,3)\|INSOLUBLE CARBONATE(12,3)\|CARBONATED SILICATE SLURRY(12,1)\|METHANEDIONE TONNE(12,1)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|UNDERGROUND REACTOR(11,2)\|BOILER ECONOMIZER(11,1)\|CHILLED SILICATE SLURRY(11,1)\|FINAL EMPLACEMENT REHABILITATION(11,1)\|INCOMING REACTANT PIPELINE(11,1)\|METHANEDIONE SCRUBBING CHAMBER(11,1)\|SILICATE SLURRY CIRCULATION(11,1)\|RAW FLUE GAS(10,6)\|METHANEDIONE CONTENT(10,2)\|FLUE GAS FILTER(9,5)\|OLIVINE(9,5)\|REACTION SOLUTION(9,5)\|AMMONIA LOSS(9,3)\|ELECTRICITY GENERATION PLANT(9,3)\|EVAPORATOR VESSEL(9,2)\|AMMONIA TONNE(9,1)\|BICARBONATE NH4HCO(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|FIN FAN COOLER(9,1)\|INCOMING SILICATE SLURRY(9,1)\|INSOLUBLE MAGNESIA(9,1)\|MAXIMIZE REGENERATION(9,1)\|METHANEDIONE ABSORPTION ZONE(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OVERLAND PIPELINE(9,1)\|REACTED SLURRY RISING(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(9,1)\|STACKED SUBCHAMBER(9,1)\|CARBON DIOXIDE(8,3)\|AMMONIA STRIPPING(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|PRESSURIZED AMMONIA PASS(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(8,1)\|POWER STATION SITE(7,7)\|CONDENSATION(7,3)\|MAGNESIUM ION(7,2)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|SLURRY FEED(7,2)\|FINAL PRODUCT SLURRY(6,5)\|MWE(6,5)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA MILLION(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBONATE MINERAL(6,1)\|CONCENTRATED AMMONIA(6,1)\|CONCENTRIC PIPE(6,1)\|CORE CARBONATION REACTION(6,1)\|FINAL PERMANENT REPOSITORY(6,1)\|GAS REMNANT(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INORGANIC COMPONENT(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|NATURAL SILICATE(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRETREATMENT EXTENT(6,1)\|PYROXENE RICH MINERAL(6,1)\|PYROXENE SILICATE METAL(6,1)\|RAW SLURRY(6,1)\|REACTED SLURRY RISE(6,1)\|RECOVERED AMMONIA(6,1)\|RESIDUAL VAPOR(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE CONVERSION(6,1)\|SLURRY REACTION(6,1)\|TRANSPORTING ORE(6,1)\|PRESSURE EXCHANGE(5,11)\|BOTTOM ASH PULVERIZATION(5,2)\|DOLOMITE(5,2)\|LIMESTONE(5,2)\|MG3SI2O(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|HOT PRODUCT PIPELINE(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|METHANEDIONE SOURCE(5,1)\|OXIDE REACTION(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|VAPORIZED AMMONIA FLOW(5,1)\|WT SLURRY(5,1)\|REACTION CHAMBER(4,4)\|METAL SILICATE SOLUTION(4,3)\|POWER STATION FLY ASH(4,3)\|SOX(4,3)\|STEAM(4,3)\|INSULATION(4,2)\|AIR PREHEATING(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA PIPE DIAMETER(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SOLUTION(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BEDROCK(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CHESHUNT MIXTURE COMPOUND(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|FINAL CARBONATE PRODUCT SLURRY(4,1)\|\|(IN6026/DELNP/2009)\|METHANEDIONE SEQUESTRATION(100,1)\|REACTION SLURRY(53,2)\|METHANEDIONE(50,3)\|METHANEDIONE SEQUESTRATION(34,1)\|METAL SILICATE ROCK(30,1)\|METAL SILICATE SLURRY(28,1)\|METAL SILICATE(22,1)\|GAS STREAM(21,1)\|REACTOR(20,1)\|METAL CARBONATE(19,1)\|\|(CA2678800)\|METHANEDIONE(100,55)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,10)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|REACTION SLURRY(91,24)\|METAL SILICATE SLURRY(90,30)\|METAL SILICATE(86,37)\|AMMONIATED SLURRY(77,5)\|MAGNESIUM RICH SILICATE(75,8)\|REACTOR(57,23)\|AMMONIA(56,76)\|AMMONIA ABSORPTION RECOVERY VESSEL(50,1)\|METAL CARBONATE(45,10)\|METAL SILICATE ROCK(45,2)\|SLURRY(38,43)\|REACTION ENHANCEMENT(37,5)\|AMMONIA ABSORPTION CHILLER(33,2)\|AMMONIA RECOVERY VESSEL(32,14)\|LIQUID PRESSURIZATION(32,1)\|FLOW PATH(31,11)\|AMMONIA ABSORPTION CHAMBER(30,5)\|OLIVINE(26,7)\|EVAPORATOR CHAMBER(26,6)\|AMMONIA WATER(23,14)\|UNDERGROUND CHAMBER(20,8)\|RESIDUAL AMMONIA SCRUBBER(20,4)\|OVERLAND AMMONIA PIPELINE(20,2)\|RECIRCULATION(20,2)\|LAGGED ABOVEGROUND PIPELINE(19,1)\|METAL CARBONATE PRODUCT(17,4)\|METHANEDIONE PERMANENT SEQUESTRATION(17,1)\|CENT METHANEDIONE(16,2)\|CHAMBER PRODUCT(16,2)\|ABSORBENT SLURRY DELUGING SPRAY(16,1)\|MINERAL CARBONATION(15,3)\|PRODUCING CHAMBER(15,2)\|AMMONIA BUBBLE(14,3)\|HUNTER VALLEY(14,2)\|TARGET METAL(14,2)\|RESIDUAL METHANEDIONE SCRUBBER(14,1)\|RETURN PIPELINE(13,5)\|CARBONATED SILICATE SLURRY(13,1)\|METHANEDIONE TONNE(13,1)\|INSOLUBLE CARBONATE(12,3)\|CHILLED SLURRY(12,2)\|HOT SILICATE SLURRY(12,2)\|INCOMING REACTIVE SLURRY(12,2)\|UNDERGROUND REACTOR(12,2)\|CARBON DIOXIDE(11,3)\|METHANEDIONE CONTENT(11,2)\|BLACK COAL MWE(11,1)\|BOILER ECONOMIZER(11,1)\|CHILLED SILICATE SLURRY(11,1)\|FINAL EMPLACEMENT REHABILITATION(11,1)\|INCOMING REACTANT PIPELINE(11,1)\|METHANEDIONE SCRUBBING CHAMBER(11,1)\|SILICATE SLURRY CIRCULATION(11,1)\|RAW FLUE GAS(10,6)\|AMMONIA LOSS(10,3)\|CARBONATION REACTION(10,2)\|EVAPORATOR VESSEL(10,2)\|FIRED ELECTRICITY GENERATION PLANT(10,2)\|AMMONIA TONNE(10,1)\|DEINKING ASH(10,1)\|ELECTRICITY GWH(10,1)\|FIN FAN COOLER(10,1)\|GLOBAL WARMING METHANEDIONE(10,1)\|INCOMING SILICATE SLURRY(10,1)\|INSOLUBLE MAGNESIA(10,1)\|MAXIMIZE REGENERATION(10,1)\|METHANEDIONE ABSORPTION ZONE(10,1)\|METHANEDIONE SINK(10,1)\|MULTISTAGE BARREL PUMP(10,1)\|OVERLAND PIPELINE(10,1)\|REACTED SLURRY RISING(10,1)\|RESIDUAL AMMONIA ABSORBER(10,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(10,1)\|STACKED SUBCHAMBER(10,1)\|FLUE GAS FILTER(9,5)\|REACTION SOLUTION(9,5)\|MINERAL MATTER(8,2)\|PUMPING ENERGY(8,2)\|SLURRY FEED(8,2)\|ABSORBER AQ(8,1)\|AMMONIA STRIPPING(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|HOT PRESSURIZED FMAL PRODUCT(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|PRESSURIZED AMMONIA PASS(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(8,1)\|POWER STATION SITE(7,7)\|CONDENSATION(7,3)\|ABSORB SURPLUS SENSIBLE HEAT(7,1)\|ALKALINE INDUSTRY RESIDUE(7,1)\|AMMONIA MILLION(7,1)\|BOOSTER PUMPING STATION(7,1)\|CARBONATE MINERAL(7,1)\|CONCENTRATED AMMONIA(7,1)\|CONCENTRIC PIPE(7,1)\|FINAL PERMANENT REPOSITORY(7,1)\|GAS REMNANT(7,1)\|GEHO PUMP(7,1)\|HOT SLURRY RISING(7,1)\|INORGANIC COMPONENT(7,1)\|MINE SITE(7,1)\|MINE VOID(7,1)\|MOIL CO2(7,1)\|MOLL CO2(7,1)\|NATURAL SILICATE(7,1)\|PAPER RECYCLING RESIDUE COMBUSTION(7,1)\|PIPELINE REACTOR CHOICE(7,1)\|PRETREATMENT EXTENT(7,1)\|PYROXENE RICH MINERAL(7,1)\|PYROXENE SILICATE METAL(7,1)\|RAW SLURRY(7,1)\|REACTED SLURRY RISE(7,1)\|RESIDUAL VAPOR(7,1)\|SCRUBBING ZONE(7,1)\|SILICATE CONVERSION(7,1)\|SLURRY REACTION(7,1)\|TRANSPORTING ORE(7,1)\|PRESSURE EXCHANGE(6,10)\|ADJACENT FLOW PATH(6,2)\|BOTTOM ASH PULVERIZATION(6,2)\|CHILLED AMMONIA WATER(6,2)\|DOLOMITE(6,2)\|LIMESTONE(6,2)\|WOLLASTONITE(6,2)\|FINAL PRODUCT SLURRY(5,4)\|REACTION CHAMBER(5,4)\|METAL SILICATE SOLUTION(5,3)\|POWER STATION FLY ASH(5,3)\|SOX(5,3)\|STEAM(5,3)\|INSULATION(5,2)\|SHELL(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|HOT PRODUCT PIPELINE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|METHANEDIONE SOURCE(5,1)\|OXIDE REACTION(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|VAPORIZED AMMONIA FLOW(5,1)\|WT SLURRY(5,1)\|AIR PREHEATING(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA PIPE DIAMETER(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SOLUTION(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CHESHUNT MIXTURE COMPOUND(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|\|(CA2678800)\|METHANEDIONE(100,55)\|METHANEDIONE SEQUESTRATION(100,14)\|GAS STREAM(100,10)\|SEQUESTRATION(100,6)\|METHANEDIONE SEQUESTRATION(100,5)\|REACTION SLURRY(91,24)\|METAL SILICATE SLURRY(90,30)\|METAL SILICATE(86,37)\|AMMONIATED SLURRY(77,5)\|MAGNESIUM RICH SILICATE(75,8)\|REACTOR(57,23)\|AMMONIA(56,76)\|AMMONIA ABSORPTION RECOVERY VESSEL(50,1)\|METAL CARBONATE(45,10)\|METAL SILICATE ROCK(45,2)\|SLURRY(38,43)\|REACTION ENHANCEMENT(37,5)\|AMMONIA ABSORPTION CHILLER(33,2)\|AMMONIA RECOVERY VESSEL(32,14)\|LIQUID PRESSURIZATION(32,1)\|FLOW PATH(31,11)\|AMMONIA ABSORPTION CHAMBER(30,5)\|OLIVINE(26,7)\|EVAPORATOR CHAMBER(26,6)\|AMMONIA WATER(23,14)\|UNDERGROUND CHAMBER(20,8)\|RESIDUAL AMMONIA SCRUBBER(20,4)\|OVERLAND AMMONIA PIPELINE(20,2)\|RECIRCULATION(20,2)\|LAGGED ABOVEGROUND PIPELINE(19,1)\|METAL CARBONATE PRODUCT(17,4)\|METHANEDIONE PERMANENT SEQUESTRATION(17,1)\|CENT METHANEDIONE(16,2)\|CHAMBER PRODUCT(16,2)\|ABSORBENT SLURRY DELUGING SPRAY(16,1)\|MINERAL CARBONATION(15,3)\|PRODUCING CHAMBER(15,2)\|AMMONIA BUBBLE(14,3)\|HUNTER VALLEY(14,2)\|TARGET METAL(14,2)\|RESIDUAL METHANEDIONE SCRUBBER(14,1)\|RETURN PIPELINE(13,5)\|CARBONATED SILICATE SLURRY(13,1)\|METHANEDIONE TONNE(13,1)\|INSOLUBLE CARBONATE(12,3)\|CHILLED SLURRY(12,2)\|HOT SILICATE SLURRY(12,2)\|INCOMING REACTIVE SLURRY(12,2)\|UNDERGROUND REACTOR(12,2)\|CARBON DIOXIDE(11,3)\|METHANEDIONE CONTENT(11,2)\|BLACK COAL MWE(11,1)\|BOILER ECONOMIZER(11,1)\|CHILLED SILICATE SLURRY(11,1)\|FINAL EMPLACEMENT REHABILITATION(11,1)\|INCOMING REACTANT PIPELINE(11,1)\|METHANEDIONE SCRUBBING CHAMBER(11,1)\|SILICATE SLURRY CIRCULATION(11,1)\|RAW FLUE GAS(10,6)\|AMMONIA LOSS(10,3)\|CARBONATION REACTION(10,2)\|EVAPORATOR VESSEL(10,2)\|FIRED ELECTRICITY GENERATION PLANT(10,2)\|AMMONIA TONNE(10,1)\|DEINKING ASH(10,1)\|ELECTRICITY GWH(10,1)\|FIN FAN COOLER(10,1)\|GLOBAL WARMING METHANEDIONE(10,1)\|INCOMING SILICATE SLURRY(10,1)\|INSOLUBLE MAGNESIA(10,1)\|MAXIMIZE REGENERATION(10,1)\|METHANEDIONE ABSORPTION ZONE(10,1)\|METHANEDIONE SINK(10,1)\|MULTISTAGE BARREL PUMP(10,1)\|OVERLAND PIPELINE(10,1)\|REACTED SLURRY RISING(10,1)\|RESIDUAL AMMONIA ABSORBER(10,1)\|RESIDUAL METHANEDIONE SCRUBBING MEDIUM(10,1)\|STACKED SUBCHAMBER(10,1)\|FLUE GAS FILTER(9,5)\|REACTION SOLUTION(9,5)\|MINERAL MATTER(8,2)\|PUMPING ENERGY(8,2)\|SLURRY FEED(8,2)\|ABSORBER AQ(8,1)\|AMMONIA STRIPPING(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HARMFUL METHANEDIONE GAS(8,1)\|HOT PRESSURIZED FMAL PRODUCT(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|PRESSURIZED AMMONIA PASS(8,1)\|RAW REACTIVE SLURRY(8,1)\|REDUCING METHANEDIONE EMISSION(8,1)\|RESIDUAL AMMONIA SCRUBBING CHAMBER(8,1)\|POWER STATION SITE(7,7)\|CONDENSATION(7,3)\|ABSORB SURPLUS SENSIBLE HEAT(7,1)\|ALKALINE INDUSTRY RESIDUE(7,1)\|AMMONIA MILLION(7,1)\|BOOSTER PUMPING STATION(7,1)\|CARBONATE MINERAL(7,1)\|CONCENTRATED AMMONIA(7,1)\|CONCENTRIC PIPE(7,1)\|FINAL PERMANENT REPOSITORY(7,1)\|GAS REMNANT(7,1)\|GEHO PUMP(7,1)\|HOT SLURRY RISING(7,1)\|INORGANIC COMPONENT(7,1)\|MINE SITE(7,1)\|MINE VOID(7,1)\|MOIL CO2(7,1)\|MOLL CO2(7,1)\|NATURAL SILICATE(7,1)\|PAPER RECYCLING RESIDUE COMBUSTION(7,1)\|PIPELINE REACTOR CHOICE(7,1)\|PRETREATMENT EXTENT(7,1)\|PYROXENE RICH MINERAL(7,1)\|PYROXENE SILICATE METAL(7,1)\|RAW SLURRY(7,1)\|REACTED SLURRY RISE(7,1)\|RESIDUAL VAPOR(7,1)\|SCRUBBING ZONE(7,1)\|SILICATE CONVERSION(7,1)\|SLURRY REACTION(7,1)\|TRANSPORTING ORE(7,1)\|PRESSURE EXCHANGE(6,10)\|ADJACENT FLOW PATH(6,2)\|BOTTOM ASH PULVERIZATION(6,2)\|CHILLED AMMONIA WATER(6,2)\|DOLOMITE(6,2)\|LIMESTONE(6,2)\|WOLLASTONITE(6,2)\|FINAL PRODUCT SLURRY(5,4)\|REACTION CHAMBER(5,4)\|METAL SILICATE SOLUTION(5,3)\|POWER STATION FLY ASH(5,3)\|SOX(5,3)\|STEAM(5,3)\|INSULATION(5,2)\|SHELL(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|GEOLOGICAL CONDITION(5,1)\|HOT PRODUCT PIPELINE(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|METHANEDIONE SOURCE(5,1)\|OXIDE REACTION(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|VAPORIZED AMMONIA FLOW(5,1)\|WT SLURRY(5,1)\|AIR PREHEATING(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA PIPE DIAMETER(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SOLUTION(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CHESHUNT MIXTURE COMPOUND(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|\|(KR10-1527365)\|CARBON DIOXIDE(100,110)\|REACTION SLURRY(100,30)\|CARBON DIOXIDE ISOLATION(100,9)\|CARBON DIOXIDE SEQUESTRATION(100,8)\|GAS STREAM(100,7)\|METAL SILICATE(88,47)\|REACTOR(72,26)\|METAL SILICATE SLURRY(64,30)\|SLURRY(48,44)\|METAL CARBONATE(47,12)\|AMMONIA(46,70)\|MAGNESIUM RICH SILICATE(46,7)\|AMMONIA ABSORPTION RECOVERY VESSEL(46,1)\|METAL AMMINE FAILURE(45,1)\|METALSILICATE(45,1)\|METAL AMMINE(40,1)\|REACTION ENHANCEMENT(38,6)\|INSOLUBLE CARBONATE(35,4)\|METAL SILICATE ROCK(35,4)\|ABSORB CARBON DIOXIDE(35,1)\|DISPERSED METAL SILICATE(35,1)\|RECOVERING AMMONIA(33,2)\|SEPARATING CARBON DIOXIDE(33,1)\|FLOW PATH(31,17)\|AMMONIA ABSORPTION CHAMBER(28,6)\|CHAMBER PRESSURIZATION(28,1)\|AMMONIA WATER(23,19)\|METER(23,1)\|NATURALLY OCCURRING ABSORPTION SOURCE(23,1)\|WHOLITE(22,1)\|CLEANING CHAMBER(21,19)\|RESIDUAL AMMONIA SCRUBBER(19,4)\|AMMONIA WATER SLURRY(19,1)\|GRINDING(19,1)\|AMMONIA RECOVERY VESSEL(18,5)\|OLIVINE(17,6)\|REACTOR CONTROL(17,5)\|METAL CARBONATE PRODUCT(17,3)\|AMMONIATED CARBONATED SILICATE SLURRY(17,1)\|CARBON DIOXIDE CHANGE(17,1)\|POWER DIRECTED EMESIS(17,1)\|SUBTERRANEAN CHAMBER(16,6)\|GRAPHITIC BURNING ELECTROGENIC GENERATOR(16,1)\|CARBON DIOXIDE REACTION(15,1)\|MINERAL CARBONIZATION(14,3)\|MINERAL SERPENTINE MG3SI2O(13,1)\|PULVERULENT COMBUSTION BOILER(13,1)\|HEAT EXCHANGER(12,24)\|AMMONIA GAS RECOVERY VESSEL(12,9)\|EVAPORATOR CHAMBER(12,5)\|RETURN PIPELINE(12,5)\|AMMONIA LOSS(11,5)\|HOT SILICATE SLURRY(11,2)\|HUNTER VALLEY(11,2)\|SUBTERRANEAN REACTOR(11,2)\|ABSORPTION SLURRY OVERFLOW SPRAY(11,1)\|BOILER ECONOMIZER(11,1)\|DESIRED TRANSFER(11,1)\|GRAPHITIC COMBUSTION GENERATOR(11,1)\|INTRODUCTION REACTANT PIPELINE(11,1)\|SILICATE SLURRY CIRCULATION(11,1)\|FLUE GAS(10,33)\|AMMONIA BUBBLE(10,2)\|CO2 ABSORBER(10,2)\|FLUE GAS FILTER(9,5)\|TONNE(9,5)\|POWER PLANT FLUE GAS(9,4)\|EVAPORATOR VESSEL(9,2)\|AMMONIA ABSORPTION COOLER(9,1)\|ELECTRICITY GWH(9,1)\|HEAT DESIRED TRANSFER(9,1)\|LIME CALCINATION(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|STACKED SUBCHAMBER(9,1)\|SUDDEN EVAPORATION RECTIFICATION VESSEL(9,1)\|POWER PLANT(8,22)\|REACTION SOLUTION(8,5)\|DOLOMITE(8,4)\|RAW FLUE GAS(8,4)\|HOT SLURRY(8,3)\|LIMESTONE(8,3)\|PERMANENT INSULATION(8,2)\|3T M3 SLURRY(8,1)\|AMMONIA CATALYSIS(8,1)\|AMMONIA PIPELINE(8,1)\|AMMONIA STRIPPING(8,1)\|COLD SILICATE SLURRY(8,1)\|COOLED SILICATE SLURRY(8,1)\|DEINKING ASH(8,1)\|ELEMENTAL IRON FE(8,1)\|KEY CARBONIZATION(8,1)\|LJUNGSTROM ROTARY(8,1)\|MULTISTAGE BARRIER(8,1)\|RAW REACTION SLURRY(8,1)\|ULTRA MAFIC ROCK(8,1)\|CARBON DIOXIDE SEPARATOR(7,3)\|WOLLASTONITE(7,3)\|ABSORPTION ZONE(7,2)\|CARBON DIOXIDE SEQUESTRANT(7,2)\|COUNTERCURRENT(7,2)\|PUMPING ENERGY(7,2)\|AMMONIUM SALT(6,2)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMINE FORMATION(6,1)\|AMMONIA BULK(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON ISOLATION ENERGY BURDEN(6,1)\|CARBONATE MINERAL(6,1)\|CLEAN SUPERNATANT(6,1)\|CLEANING MEDIUM CIRCULATION(6,1)\|CONCENTRIC PIPE(6,1)\|DISSOLVE TARGET(6,1)\|ELECTROMAGNETIC PRECIPITATE(6,1)\|ENERGY MWT(6,1)\|FIN FAN(6,1)\|FINE UNDERGROUND CHAMBER(6,1)\|GEHO PUMP(6,1)\|GENERATOR FIRING(6,1)\|GRADUAL MANNER RESULT(6,1)\|INTRODUCED REACTIVE SLURRY(6,1)\|INTRODUCED SILICATE SLURRY(6,1)\|MAGNESIUM DISSOLUTION(6,1)\|MEGAWATT HOUR TON(6,1)\|MILD REAGENT(6,1)\|MILLION AMMONIA(6,1)\|MINING SITE(6,1)\|MWE COAL(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PARTICULATE CLEANING(6,1)\|RAW SLURRY(6,1)\|RICH MINERAL(6,1)\|SILICATE SLURRY DENSITY(6,1)\|SITE CARBONIZATION(6,1)\|SLURRY REACTION(6,1)\|SUBTERRANEAN PROCESSING VESSEL(6,1)\|THROTTLING VALVE(6,1)\|TOTALITY PRODUCT SLURRY(6,1)\|WATER ABSORBENT(6,1)\|POWER PLANT SITE(5,4)\|CARBON DIOXIDE EMISSION(5,2)\|DOLIME(5,2)\|LIPID CONDITION(5,2)\|AMMONIA COMBINED SLURRY(5,1)\|CALCIUM CA(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENTRIFUGAL PUMP FORMAT(5,1)\|CIRCULATION ENOUGH NATURAL PROPORTION(5,1)\|CLASSIFICATION(5,1)\|COAL FUEL(5,1)\|COLD SLURRY(5,1)\|COOLED SLURRY(5,1)\|DIVALENT IRON(5,1)\|EMISSION END(5,1)\|FINAL INSTALLATION SITE(5,1)\|FINAL PERMANENT RESERVOIR(5,1)\|FLOOR ASH(5,1)\|FRICTION LOSS(5,1)\|GENERATOR SITE(5,1)\|GROUND AMMONIA(5,1)\|GROUND PIPELINE(5,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(5,1)\|MAGNESIUM CARBONATE EXTRACTION(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM MG(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|MAXIMIZE GENERATION(5,1)\|ORE SITE(5,1)\|PERMANENT PLACEMENT(5,1)\|PIPE REACTOR(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PRETREATMENT EXTENT(5,1)\|PUMPING CAPACITY(5,1)\|RESIDUAL VAPOR(5,1)\|SERPENTINE MINERAL ACID SITE(5,1)\|SLOW IDEAL(5,1)\|SLURRY COOLING(5,1)\|SLURRY FEED(5,1)\|STATIONARY PLANT(5,1)\|STRATEGIC LOCATION(5,1)\|STRIP AMMONIA(5,1)\|THICK SLURRY(5,1)\|UNDERGOING TREATMENT(5,1)\|CARBON DIOXIDE SEQUESTRATION(4,3)\|FINAL PRODUCT SLURRY(4,3)\|METAL SILICATE SOLUTION(4,3)\|SOX(4,3)\|ULTRASOUND(4,3)\|2CO3AMMONIA(4,1)\|2CO3BASED(4,1)\|ABSORB EXCESS SENSIBLE HEAT(4,1)\|AMMONIA GAS BUBBLE(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA PIPE DIAMETER(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIA SALT SOLUTION(4,1)\|AMMONIUM CARBONATE COMPOUND(4,1)\|ANNULUS(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BOTTOM ASH PULVERIZATION(4,1)\|CARBAMATE(4,1)\|CARBON DIOXIDE CLEANING CHAMBER(4,1)\|CARBON DIOXIDE PERMANENT ISOLATION(4,1)\|CARBON DIOXIDE SCRUBBER(4,1)\|CARBON DIOXIDE SINK(4,1)\|CASIO3PAUL(4,1)\|CLEAN FLUE GAS(4,1)\|CLEANING REGION(4,1)\|CM3WILL(4,1)\|CONCENTRIC INNER(4,1)\|CONTINENT(4,1)\|CRUSHING(4,1)\|DOWNSTREAM GAS(4,1)\|ECONOMIC PERSPECTIVE(4,1)\|EXOTHERMIC CARBON DIOXIDE(4,1)\|\|(KR10-2009-0125109)\|CARBON DIOXIDE(100,114)\|AMMONIA(100,72)\|METAL SILICATE(100,54)\|SLURRY(100,47)\|METAL SILICATE SLURRY(100,35)\|PIPELINE(100,35)\|REACTION SLURRY(100,33)\|AMMONIA WATER(100,22)\|METAL CARBONATE(100,15)\|CARBON DIOXIDE SEQUESTRATION(100,9)\|EVAPORATOR(100,8)\|ABSORPTION(100,6)\|METAL SILICATE ROCK(100,5)\|AMMONIA ABSORPTION(100,4)\|CARBON DIOXIDE SEQUESTRATION(100,4)\|GAS STREAM(100,4)\|METAL SILICATE ROCK SLURRY(100,4)\|SEQUESTRATION(100,4)\|ABSORPTION(100,1)\|COOLING PATTERN(100,1)\|LIQUID PRESSURIZATION(100,1)\|AMMONIATED SLURRY(72,1)\|MAGNESIUM RICH SILICATE(68,9)\|REACTOR(56,24)\|REACTION ENHANCEMENT(41,7)\|DISSOLVE TARGET(40,2)\|AMMONIA ABSORPTION RECOVERY VESSEL(40,1)\|METAL AMMINE FAILURE(39,1)\|AMMONIA ABSORPTION COOLER(35,2)\|AMMONIA ABSORPTION CHAMBER(34,7)\|METAL AMMINE(34,1)\|INSOLUBLE CARBONATE(30,4)\|AMMONIA SALT(30,3)\|ABSORB CARBON DIOXIDE(30,1)\|DISPERSED METAL SILICATE(30,1)\|RECOVERING AMMONIA(28,2)\|FLOW PATH(27,14)\|REACTOR CONTROL(26,6)\|SEQUESTRATION CARBON DIOXIDE(24,1)\|CLEANING CHAMBER(23,20)\|AMMONIA LOSS(23,6)\|AMMONIA COMBINED SLURRY(23,2)\|GRINDING(23,2)\|EVAPORATOR CHAMBER(21,6)\|COOLED SLURRY(21,2)\|OLIVINE(20,7)\|CARBON SEQUESTRATION(20,6)\|METER(20,1)\|NATURALLY OCCURRING ABSORPTION SOURCE(20,1)\|WHISTONITE(20,1)\|CARBON DIOXIDE ISOLATION(17,8)\|HEAT EXCHANGER(16,26)\|RESIDUAL AMMONIA SCRUBBER(16,4)\|TARGET METAL(16,4)\|AMMONIA METAL SILICATE SLURRY(16,2)\|AMMONIA RECOVERY VESSEL(15,5)\|METAL CARBONATE PRODUCT(15,3)\|SILICATE METAL(15,2)\|AMMONIATED CARBONATED SILICATE SLURRY(15,1)\|CARBON DIOXIDE CHANGE(15,1)\|POWER DIRECTED EMESIS(15,1)\|SUBTERRANEAN CHAMBER(14,6)\|GRAPHITIC BURNING ELECTROGENIC GENERATOR(14,1)\|CHAMBER PRODUCT(13,2)\|MINERAL CARBONIZATION(12,3)\|PRODUCING CHAMBER(12,2)\|CARBON SEQUESTRATION(11,3)\|MINERAL SERPENTINE MG3SI2O(11,1)\|PULVERULENT COMBUSTION BOILER(11,1)\|FLUE GAS(10,34)\|POWER PLANT(10,24)\|AMMONIA GAS RECOVERY VESSEL(10,9)\|RETURN PIPELINE(10,5)\|COOLED AMMONIA WATER(10,3)\|HOT SILICATE SLURRY(10,2)\|HUNTER VALLEY(10,2)\|SUBTERRANEAN REACTOR(10,2)\|AMMONIA BUBBLE(9,2)\|CO2 ABSORBER(9,2)\|ABSORPTION SLURRY OVERFLOW SPRAY(9,1)\|BOILER ECONOMIZER(9,1)\|DESIRED TRANSFER(9,1)\|GRAPHITIC COMBUSTION GENERATOR(9,1)\|INTRODUCTION REACTANT PIPELINE(9,1)\|SILICATE SLURRY CIRCULATION(9,1)\|POWER PLANT FLUE GAS(8,4)\|EVAPORATOR VESSEL(8,2)\|ELECTRICITY GWH(8,1)\|HEAT DESIRED TRANSFER(8,1)\|LIME CALCINATION(8,1)\|RESIDUAL AMMONIA ABSORBER(8,1)\|STACKED SUBCHAMBER(8,1)\|SUDDEN EVAPORATION RECTIFICATION VESSEL(8,1)\|FLUE GAS FILTER(7,5)\|TONNE(7,5)\|DOLOMITE(7,4)\|RAW FLUE GAS(7,4)\|HOT SLURRY(7,3)\|LIMESTONE(7,3)\|PERMANENT INSULATION(7,2)\|3T M3 SLURRY(7,1)\|AMMONIA CATALYSIS(7,1)\|AMMONIA PIPELINE(7,1)\|AMMONIA STRIPPING(7,1)\|COLD SILICATE SLURRY(7,1)\|COOLED SILICATE SLURRY(7,1)\|DEINKING ASH(7,1)\|ELEMENTAL IRON FE(7,1)\|KEY CARBONIZATION(7,1)\|LJUNGSTROM ROTARY(7,1)\|MULTISTAGE BARRIER(7,1)\|RAW REACTION SLURRY(7,1)\|ULTRA MAFIC ROCK(7,1)\|REACTION SOLUTION(6,5)\|CARBON DIOXIDE SEPARATOR(6,3)\|REACTION STEP(6,3)\|WOLLASTONITE(6,3)\|ABSORPTION ZONE(6,2)\|CARBON DIOXIDE SEQUESTRANT(6,2)\|PUMPING ENERGY(6,2)\|AMMONIUM SALT(5,2)\|CARBON DIOXIDE EMISSION(5,2)\|COUNTERCURRENT(5,2)\|DOLIME(5,2)\|LIPID CONDITION(5,2)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMINE FORMATION(5,1)\|AMMONIA BULK(5,1)\|AMMONIA SLIP(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBON ISOLATION ENERGY BURDEN(5,1)\|CARBONATE MINERAL(5,1)\|CLEAN SUPERNATANT(5,1)\|CLEANING MEDIUM CIRCULATION(5,1)\|CONCENTRIC PIPE(5,1)\|ELECTROMAGNETIC PRECIPITATE(5,1)\|ENERGY MWT(5,1)\|FINE UNDERGROUND CHAMBER(5,1)\|GEHO PUMP(5,1)\|GENERATOR FIRING(5,1)\|GRADUAL MANNER RESULT(5,1)\|INTRODUCED REACTIVE SLURRY(5,1)\|INTRODUCED SILICATE SLURRY(5,1)\|MAGNESIUM DISSOLUTION(5,1)\|MEGAWATT HOUR TON(5,1)\|MILD REAGENT(5,1)\|MILLION AMMONIA(5,1)\|MINING SITE(5,1)\|MWE COAL(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PARTICULATE CLEANING(5,1)\|RAW SLURRY(5,1)\|RICH MINERAL(5,1)\|SILICATE SLURRY DENSITY(5,1)\|SITE CARBONIZATION(5,1)\|SLURRY REACTION(5,1)\|SUBTERRANEAN PROCESSING VESSEL(5,1)\|THROTTLING VALVE(5,1)\|TOTALITY PRODUCT SLURRY(5,1)\|WATER ABSORBENT(5,1)\|LIQUID STATE(4,5)\|OVERCOAT(4,4)\|POWER PLANT SITE(4,4)\|FINAL PRODUCT SLURRY(4,3)\|METAL SILICATE SOLUTION(4,3)\|SOX(4,3)\|AGITATION(4,2)\|CALCIUM CA(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENTRIFUGAL PUMP FORMAT(4,1)\|CIRCULATION ENOUGH NATURAL PROPORTION(4,1)\|CLASSIFICATION(4,1)\|COAL FUEL(4,1)\|COLD SLURRY(4,1)\|DIVALENT IRON(4,1)\|EMISSION END(4,1)\|FINAL INSTALLATION SITE(4,1)\|FINAL PERMANENT RESERVOIR(4,1)\|FLOOR ASH(4,1)\|FRICTION LOSS(4,1)\|GENERATOR SITE(4,1)\|GROUND AMMONIA(4,1)\|GROUND PIPELINE(4,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(4,1)\|MAGNESIUM CARBONATE EXTRACTION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM MG(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAXIMIZE GENERATION(4,1)\|ORE SITE(4,1)\|OXIDE REACTION(4,1)\|PERMANENT PLACEMENT(4,1)\|PIPE REACTOR(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PRETREATMENT EXTENT(4,1)\|PUMPING CAPACITY(4,1)\|RESIDUAL VAPOR(4,1)\|SERPENTINE MINERAL ACID SITE(4,1)\|SLOW IDEAL(4,1)\|SLURRY COOLING(4,1)\|SLURRY FEED(4,1)\|STATIONARY PLANT(4,1)\|STRATEGIC LOCATION(4,1)\|STRIP AMMONIA(4,1)\|THICK SLURRY(4,1)\|UNDERGOING TREATMENT(4,1)\|REACTION CHAMBER(3,4)\|2CO3AMMONIA(3,1)\|2CO3BASED(3,1)\|ABSORB EXCESS SENSIBLE HEAT(3,1)\|AMMONIA GAS BUBBLE(3,1)\|AMMONIA PIPE DIAMETER(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIA SALT SOLUTION(3,1)\|AMMONIUM CARBONATE COMPOUND(3,1)\|ANNULUS(3,1)\|BAYSWATER POWER STATION(3,1)\|BICARBONATE(3,1)\|BIOMASS(3,1)\|BOTTOM ASH PULVERIZATION(3,1)\|CARBAMATE(3,1)\|CARBON DIOXIDE CLEANING CHAMBER(3,1)\|CARBON DIOXIDE PERMANENT ISOLATION(3,1)\|CARBON DIOXIDE SCRUBBER(3,1)\|CARBON DIOXIDE SINK(3,1)\|CASIO3PAUL(3,1)\|CLEAN FLUE GAS(3,1)\|CLEANING REGION(3,1)\|CM3WILL(3,1)\|\|(AU2008217572)\|METAL SILICATE SLURRY(100,32)\|REACTION SLURRY(92,24)\|METAL SILICATE(80,38)\|LIMESTONE PULVERIZATION(79,1)\|AMMONIATED SLURRY(71,5)\|METAL CARBONATE(68,13)\|MAGNESIUM RICH SILICATE(61,7)\|PERMANENT SEQUESTRATION(55,2)\|REACTOR(52,25)\|REACTION ENHANCEMENT(51,6)\|SEQUESTERING CARBON DIOXIDE(51,3)\|COAL FUEL(51,1)\|CARBON DIOXIDE(50,66)\|PIPELINE(50,28)\|SLURRY(45,43)\|GAS STREAM(45,11)\|AMMONIA ABSORPTION RECOVERY VESSEL(45,1)\|FLOW PATH(43,12)\|AMMONIA(41,66)\|RECOVERING AMMONIA(40,8)\|NATURALLY OCCURRING SINK(40,1)\|SCRUBBING CHAMBER(37,17)\|INSOLUBLE CARBONATE(35,4)\|POWER THIRSTY CLIMATE(35,1)\|RETURN PATHWAY(34,2)\|DOLOMITE(33,4)\|AMMONIA ABSORPTION CHILLER(31,2)\|CARBON SEQUESTRATION(29,9)\|AMMONIA WATER(28,13)\|REACTOR CONTROL(28,1)\|POWER STATION BOILER(26,1)\|METAL SILICATE ROCK(22,2)\|SEQUESTER CARBON DIOXIDE(22,2)\|CARBON SEQUESTRATION(21,3)\|CARBON DIOXIDE REMOVAL(21,2)\|UNDERGROUND CHAMBER(20,9)\|DUTY(20,2)\|AMMONIA RECOVERY VESSEL(19,14)\|OVERLAND AMMONIA PIPELINE(19,2)\|CARBON DIOXIDE SEQUESTRATION(18,23)\|PRESSURIZED LIQUID AMMONIA(18,3)\|OLIVINE(17,6)\|CARBON CAPTURE(17,1)\|LAGGED ABOVEGROUND PIPELINE(17,1)\|FLY ASH(15,7)\|AMMONIA ABSORPTION CHAMBER(15,5)\|POWER STATION FLY ASH(15,4)\|CHAMBER PRODUCT(15,2)\|POWER STATION(14,26)\|PRODUCING CHAMBER(14,2)\|ABSORBENT SLURRY DELUGING SPRAY(14,1)\|MINERAL CARBONATION(13,3)\|HUNTER VALLEY(13,2)\|CARBON DIOXIDE SEQUESTRATION(12,7)\|EVAPORATOR CHAMBER(12,5)\|RETURN PIPELINE(12,5)\|ABSORBING AMMONIA(12,3)\|CARBONATED SILICATE SLURRY(12,1)\|CHILLED SLURRY(11,2)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|UNDERGROUND REACTOR(11,2)\|BLACK COAL MWE(10,1)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|INCOMING REACTANT PIPELINE(10,1)\|SILICATE SLURRY CIRCULATION(10,1)\|RAW FLUE GAS(9,6)\|FLUE GAS FILTER(9,5)\|REACTION SOLUTION(9,5)\|CARBONATION REACTION(9,2)\|EVAPORATOR VESSEL(9,2)\|FIRED ELECTRICITY GENERATION PLANT(9,2)\|AMMONIA TONNE(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|INCOMING SILICATE SLURRY(9,1)\|MAXIMIZE REGENERATION(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OVERLAND PIPELINE(9,1)\|REACTED SLURRY RISING(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|STACKED SUBCHAMBER(9,1)\|ABSORBER AQ(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HOT PRESSURIZED FMAL PRODUCT(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|RAW REACTIVE SLURRY(8,1)\|TONNE AMMONIA(8,1)\|POWER STATION SITE(7,7)\|CARBON DIOXIDE TONNE(7,2)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|SLURRY FEED(7,2)\|CONDENSATION(6,3)\|CENT CARBON DIOXIDE(6,2)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA CONCENTRATION(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(6,1)\|CARBONATE MINERAL FINAL EMPLACEMENT(6,1)\|CONCENTRIC PIPE(6,1)\|FINAL PERMANENT REPOSITORY(6,1)\|GAS REMNANT(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INORGANIC COMPONENT(6,1)\|INSOLUBLE CARBONATE NATURE(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|NATURAL SILICATE(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRETREATMENT EXTENT(6,1)\|PYROXENE RICH MINERAL(6,1)\|PYROXENE SILICATE METAL(6,1)\|RAW SLURRY(6,1)\|REACTED SLURRY RISE(6,1)\|RESIDUAL VAPOR(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE CONVERSION(6,1)\|SLURRY REACTION(6,1)\|TRANSPORTING ORE(6,1)\|FINAL PRODUCT SLURRY(5,4)\|ADJACENT FLOW PATH(5,2)\|BOTTOM ASH PULVERIZATION(5,2)\|CHILLED AMMONIA WATER(5,2)\|LIMESTONE(5,2)\|RESIDUAL AMMONIA SCRUBBER DETAIL(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|AMMONIA VAPOR FLOW(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|HOT PRODUCT PIPELINE(5,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(5,1)\|KEEPING UP(5,1)\|LIQUID PRESSURIZATION(5,1)\|MAGNESIUM CARBONATE EXTRACTION(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|OXIDE REACTION(5,1)\|PERFOI RING(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|WT SLURRY(5,1)\|AMMONIUM SALT(4,4)\|REACTION CHAMBER(4,4)\|SOX(4,3)\|INSULATION(4,2)\|LIQUID AMMONIA RECOVERY(4,2)\|SHELL(4,2)\|SINGLE INTEGRATED(4,2)\|AIR PREHEATING(4,1)\|AMMONIA ABSORBER(4,1)\|AMMONIA GAS PIPE DIAMETER(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIUM CARBONATE COMPOUND(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CARBON DIOXIDE ABSORPTION ZONE(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|GAS LIQUID SEPARATOR(4,1)\|GEOLOGICAL CONDITION PERMIT(4,1)\|HARMFUL CARBON DIOXIDE GAS(4,1)\|HEAT BALANCE FIGURE(4,1)\|HEAT CONSERVATION(4,1)\|ID MOL(4,1)\|INDICATIVE MASS(4,1)\|LATTER CONTINUING(4,1)\|LIDDELL POWER STATION(4,1)\|\|(AU2008217572)\|METAL SILICATE SLURRY(100,32)\|REACTION SLURRY(92,24)\|METAL SILICATE(80,38)\|LIMESTONE PULVERIZATION(79,1)\|AMMONIATED SLURRY(71,5)\|METAL CARBONATE(68,13)\|MAGNESIUM RICH SILICATE(61,7)\|PERMANENT SEQUESTRATION(55,2)\|REACTOR(52,25)\|REACTION ENHANCEMENT(51,6)\|SEQUESTERING CARBON DIOXIDE(51,3)\|COAL FUEL(51,1)\|CARBON DIOXIDE(50,66)\|PIPELINE(50,28)\|SLURRY(45,43)\|GAS STREAM(45,11)\|AMMONIA ABSORPTION RECOVERY VESSEL(45,1)\|FLOW PATH(43,12)\|AMMONIA(41,66)\|RECOVERING AMMONIA(40,8)\|NATURALLY OCCURRING SINK(40,1)\|SCRUBBING CHAMBER(37,17)\|INSOLUBLE CARBONATE(35,4)\|POWER THIRSTY CLIMATE(35,1)\|RETURN PATHWAY(34,2)\|DOLOMITE(33,4)\|AMMONIA ABSORPTION CHILLER(31,2)\|CARBON SEQUESTRATION(29,9)\|AMMONIA WATER(28,13)\|REACTOR CONTROL(28,1)\|POWER STATION BOILER(26,1)\|METAL SILICATE ROCK(22,2)\|SEQUESTER CARBON DIOXIDE(22,2)\|CARBON SEQUESTRATION(21,3)\|CARBON DIOXIDE REMOVAL(21,2)\|UNDERGROUND CHAMBER(20,9)\|DUTY(20,2)\|AMMONIA RECOVERY VESSEL(19,14)\|OVERLAND AMMONIA PIPELINE(19,2)\|CARBON DIOXIDE SEQUESTRATION(18,23)\|PRESSURIZED LIQUID AMMONIA(18,3)\|OLIVINE(17,6)\|CARBON CAPTURE(17,1)\|LAGGED ABOVEGROUND PIPELINE(17,1)\|FLY ASH(15,7)\|AMMONIA ABSORPTION CHAMBER(15,5)\|POWER STATION FLY ASH(15,4)\|CHAMBER PRODUCT(15,2)\|POWER STATION(14,26)\|PRODUCING CHAMBER(14,2)\|ABSORBENT SLURRY DELUGING SPRAY(14,1)\|MINERAL CARBONATION(13,3)\|HUNTER VALLEY(13,2)\|CARBON DIOXIDE SEQUESTRATION(12,7)\|EVAPORATOR CHAMBER(12,5)\|RETURN PIPELINE(12,5)\|ABSORBING AMMONIA(12,3)\|CARBONATED SILICATE SLURRY(12,1)\|CHILLED SLURRY(11,2)\|HOT SILICATE SLURRY(11,2)\|INCOMING REACTIVE SLURRY(11,2)\|UNDERGROUND REACTOR(11,2)\|BLACK COAL MWE(10,1)\|BOILER ECONOMIZER(10,1)\|CHILLED SILICATE SLURRY(10,1)\|INCOMING REACTANT PIPELINE(10,1)\|SILICATE SLURRY CIRCULATION(10,1)\|RAW FLUE GAS(9,6)\|FLUE GAS FILTER(9,5)\|REACTION SOLUTION(9,5)\|CARBONATION REACTION(9,2)\|EVAPORATOR VESSEL(9,2)\|FIRED ELECTRICITY GENERATION PLANT(9,2)\|AMMONIA TONNE(9,1)\|DEINKING ASH(9,1)\|ELECTRICITY GWH(9,1)\|INCOMING SILICATE SLURRY(9,1)\|MAXIMIZE REGENERATION(9,1)\|MULTISTAGE BARREL PUMP(9,1)\|OVERLAND PIPELINE(9,1)\|REACTED SLURRY RISING(9,1)\|RESIDUAL AMMONIA ABSORBER(9,1)\|STACKED SUBCHAMBER(9,1)\|ABSORBER AQ(8,1)\|EMPLACEMENT SITE(8,1)\|FIRED BOILER(8,1)\|HOT PRESSURIZED FMAL PRODUCT(8,1)\|LJUNGSTROM ROTARY(8,1)\|PERMANENT EMPLACEMENT(8,1)\|RAW REACTIVE SLURRY(8,1)\|TONNE AMMONIA(8,1)\|POWER STATION SITE(7,7)\|CARBON DIOXIDE TONNE(7,2)\|MINERAL MATTER(7,2)\|PUMPING ENERGY(7,2)\|SLURRY FEED(7,2)\|CONDENSATION(6,3)\|CENT CARBON DIOXIDE(6,2)\|ABSORB SURPLUS SENSIBLE HEAT(6,1)\|ALKALINE INDUSTRY RESIDUE(6,1)\|AMMONIA CONCENTRATION(6,1)\|AMMONIA SLIP(6,1)\|BOOSTER PUMPING STATION(6,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(6,1)\|CARBONATE MINERAL FINAL EMPLACEMENT(6,1)\|CONCENTRIC PIPE(6,1)\|FINAL PERMANENT REPOSITORY(6,1)\|GAS REMNANT(6,1)\|GEHO PUMP(6,1)\|HOT SLURRY RISING(6,1)\|INORGANIC COMPONENT(6,1)\|INSOLUBLE CARBONATE NATURE(6,1)\|MINE SITE(6,1)\|MINE VOID(6,1)\|NATURAL SILICATE(6,1)\|PAPER RECYCLING RESIDUE COMBUSTION(6,1)\|PIPELINE REACTOR CHOICE(6,1)\|PRETREATMENT EXTENT(6,1)\|PYROXENE RICH MINERAL(6,1)\|PYROXENE SILICATE METAL(6,1)\|RAW SLURRY(6,1)\|REACTED SLURRY RISE(6,1)\|RESIDUAL VAPOR(6,1)\|SCRUBBING ZONE(6,1)\|SILICATE CONVERSION(6,1)\|SLURRY REACTION(6,1)\|TRANSPORTING ORE(6,1)\|FINAL PRODUCT SLURRY(5,4)\|ADJACENT FLOW PATH(5,2)\|BOTTOM ASH PULVERIZATION(5,2)\|CHILLED AMMONIA WATER(5,2)\|LIMESTONE(5,2)\|RESIDUAL AMMONIA SCRUBBER DETAIL(5,2)\|WOLLASTONITE(5,2)\|ABUNDANCE(5,1)\|AGITATION EQUIPMENT(5,1)\|AMMONIA SALT(5,1)\|AMMONIA VAPOR FLOW(5,1)\|CARBONATE SILICA SLURRY(5,1)\|CENT NITROGEN(5,1)\|CLASSIFICATION(5,1)\|CLEAR SUPERNATANT(5,1)\|COLD SLURRY(5,1)\|CONTINENTAL LAND MASS(5,1)\|COUNTERCURRENT HEAT EXCHANGER(5,1)\|DIVALENT IRON(5,1)\|FLASH RECTIFYING VESSEL(5,1)\|GAS TONNE(5,1)\|HOT PRODUCT PIPELINE(5,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(5,1)\|KEEPING UP(5,1)\|LIQUID PRESSURIZATION(5,1)\|MAGNESIUM CARBONATE EXTRACTION(5,1)\|MAGNESIUM ION(5,1)\|MAGNESIUM RICH SILICATE MINERAL(5,1)\|OXIDE REACTION(5,1)\|PERFOI RING(5,1)\|PIPE REACTOR(5,1)\|PIPELINE HEAT EXCHANGER(5,1)\|PIPELINE REACTOR CONFIGURATION(5,1)\|PREPROCESSING(5,1)\|PUMPING CAPACITY(5,1)\|RECUPERATIVE HEAT EXCHANGER(5,1)\|SLURRY COOLING(5,1)\|SLURRY UPFLOW RATE(5,1)\|STRATEGIC LOCATION(5,1)\|WT SLURRY(5,1)\|AMMONIUM SALT(4,4)\|REACTION CHAMBER(4,4)\|SOX(4,3)\|INSULATION(4,2)\|LIQUID AMMONIA RECOVERY(4,2)\|SHELL(4,2)\|SINGLE INTEGRATED(4,2)\|AIR PREHEATING(4,1)\|AMMONIA ABSORBER(4,1)\|AMMONIA GAS PIPE DIAMETER(4,1)\|AMMONIA METAL SILICATE SLURRY(4,1)\|AMMONIA RICH SOLUTION(4,1)\|AMMONIUM CARBONATE COMPOUND(4,1)\|ANNULUS(4,1)\|ARRIVAL PRESSURE(4,1)\|BAYSWATER POWER STATION(4,1)\|BICARBONATE(4,1)\|BIOMASS(4,1)\|BUOYANCY(4,1)\|CARBAMATE(4,1)\|CARBON DIOXIDE ABSORPTION ZONE(4,1)\|CHILLED GROUND METAL SILICATE(4,1)\|CHILLED SOLUTION(4,1)\|CIRCULATION NATURAL RATE(4,1)\|CLADDING(4,1)\|CLEAN FLUE GAS(4,1)\|CONCENTRIC INNER PIPE(4,1)\|COOL GAS(4,1)\|CRUSHING(4,1)\|DESTRUCTION(4,1)\|DISCHARGE END(4,1)\|DOLIME(4,1)\|DOMINANT METAL(4,1)\|DOWNSTREAM GAS(4,1)\|EARTH METAL SILICATE ROCK(4,1)\|ELECTROSTATIC PRECIPITATOR(4,1)\|GAS LIQUID SEPARATOR(4,1)\|GEOLOGICAL CONDITION PERMIT(4,1)\|HARMFUL CARBON DIOXIDE GAS(4,1)\|HEAT BALANCE FIGURE(4,1)\|HEAT CONSERVATION(4,1)\|ID MOL(4,1)\|INDICATIVE MASS(4,1)\|LATTER CONTINUING(4,1)\|LIDDELL POWER STATION(4,1)\|\|(AU2009250983)\|METAL SILICATE SLURRY(100,36)\|REACTION SLURRY(83,26)\|METAL SILICATE(82,44)\|LIMESTONE PULVERIZATION(65,1)\|MAGNESIUM RICH SILICATE(62,9)\|METAL CARBONATE(58,14)\|AMMONIATED SLURRY(58,5)\|AMMONIA(48,71)\|PERMANENT SEQUESTRATION(45,2)\|CARBON DIOXIDE(43,69)\|REACTOR(43,26)\|EVAPORATOR(43,8)\|REACTION ENHANCEMENT(42,6)\|SEQUESTERING CARBON DIOXIDE(42,3)\|COAL FUEL(42,1)\|PIPELINE(41,28)\|GAS STREAM(40,12)\|SLURRY(39,45)\|METAL SILICATE ROCK(37,3)\|AMMONIA ABSORPTION RECOVERY VESSEL(37,1)\|SCRUBBING CHAMBER(36,18)\|FLOW PATH(35,12)\|RECOVERING AMMONIA(33,8)\|AMMONIA ABSORPTION CHAMBER(33,7)\|NATURALLY OCCURRING SINK(33,1)\|LIQUID PRESSURIZATION(30,2)\|AMMONIA WATER(29,15)\|INSOLUBLE CARBONATE(28,4)\|RETURN PATHWAY(28,2)\|POWER THIRSTY CLIMATE(28,1)\|DOLOMITE(27,4)\|CHILLED SLURRY(27,3)\|AMMONIA ABSORPTION CHILLER(25,2)\|CARBON SEQUESTRATION(24,9)\|PYROXENE SILICATE METAL(23,2)\|REACTOR CONTROL(23,1)\|POWER STATION BOILER(22,1)\|CARBON DIOXIDE SEQUESTRATION(19,24)\|OLIVINE(19,7)\|EVAPORATOR CHAMBER(19,6)\|AMMONIA ABSORPTION(18,2)\|CARBON DIOXIDE REMOVAL(18,2)\|SEQUESTER CARBON DIOXIDE(18,2)\|CARBON SEQUESTRATION(17,3)\|DUTY(17,2)\|AMMONIA RECOVERY VESSEL(16,14)\|UNDERGROUND CHAMBER(16,9)\|PRESSURIZED LIQUID AMMONIA(15,3)\|OVERLAND AMMONIA PIPELINE(15,2)\|RECIRCULATION(15,2)\|CARBON DIOXIDE SEQUESTRATION(14,8)\|CHILLED AMMONIA WATER(14,3)\|ABSORPTION(14,2)\|CARBON CAPTURE(14,1)\|LAGGED ABOVEGROUND PIPELINE(14,1)\|FLY ASH(12,7)\|POWER STATION FLY ASH(12,4)\|CHAMBER PRODUCT(12,2)\|ABSORBENT SLURRY DELUGING SPRAY(12,1)\|POWER STATION(11,26)\|AMMONIUM SALT(11,5)\|MINERAL CARBONATION(11,3)\|PRODUCING CHAMBER(11,2)\|ABSORBING AMMONIA(10,3)\|HUNTER VALLEY(10,2)\|TARGET METAL(10,2)\|RETURN PIPELINE(9,5)\|HOT SILICATE SLURRY(9,2)\|INCOMING REACTIVE SLURRY(9,2)\|TONNE CO2 GWH(9,2)\|UNDERGROUND REACTOR(9,2)\|CARBONATED SILICATE SLURRY(9,1)\|RAW FLUE GAS(8,6)\|BLACK COAL MWE(8,1)\|BOILER ECONOMIZER(8,1)\|CHILLED SILICATE SLURRY(8,1)\|INCOMING REACTANT PIPELINE(8,1)\|MAFIC ROCK(8,1)\|SILICATE SLURRY CIRCULATION(8,1)\|FLUE GAS FILTER(7,5)\|REACTION SOLUTION(7,5)\|CARBONATION REACTION(7,2)\|CO2 ABSORBER(7,2)\|EVAPORATOR VESSEL(7,2)\|FIRED ELECTRICITY GENERATION PLANT(7,2)\|AMMONIA TONNE(7,1)\|DEINKING ASH(7,1)\|ELECTRICITY GWH(7,1)\|FIN FAN COOLER(7,1)\|INCOMING SILICATE SLURRY(7,1)\|MAXIMIZE REGENERATION(7,1)\|MULTISTAGE BARREL PUMP(7,1)\|OVERLAND PIPELINE(7,1)\|REACTED SLURRY RISING(7,1)\|RESIDUAL AMMONIA ABSORBER(7,1)\|STACKED SUBCHAMBER(7,1)\|ULTRAMANE ROCK(7,1)\|CARBON DIOXIDE TONNE(6,2)\|MINERAL MATTER(6,2)\|PUMPING ENERGY(6,2)\|SLURRY FEED(6,2)\|ABSORBER AQ(6,1)\|EMPLACEMENT SITE(6,1)\|FIRED BOILER(6,1)\|ID MON CO2(6,1)\|LJUNGSTROM ROTARY(6,1)\|PERMANENT EMPLACEMENT(6,1)\|RAW REACTIVE SLURRY(6,1)\|TONNE AMMONIA(6,1)\|POWER STATION SITE(5,7)\|CONDENSATION(5,3)\|CENT CARBON DIOXIDE(5,2)\|ABSORB SURPLUS SENSIBLE HEAT(5,1)\|ALKALINE INDUSTRY RESIDUE(5,1)\|AMMONIA CONCENTRATION(5,1)\|AMMONIA SLIP(5,1)\|BOOSTER PUMPING STATION(5,1)\|CARBON DIOXIDE PERMANENT SEQUESTRATION(5,1)\|CARBONATE MINERAL FINAL EMPLACEMENT(5,1)\|CONCENTRIC PIPE(5,1)\|FINAL PERMANENT REPOSITORY(5,1)\|GAS REMNANT(5,1)\|GEHO PUMP(5,1)\|HOT SLURRY RISING(5,1)\|INORGANIC COMPONENT(5,1)\|INSOLUBLE CARBONATE NATURE(5,1)\|MINE SITE(5,1)\|MINE VOID(5,1)\|MORL CO2(5,1)\|NATURAL SILICATE(5,1)\|PAPER RECYCLING RESIDUE COMBUSTION(5,1)\|PIPELINE REACTOR CHOICE(5,1)\|PRETREATMENT EXTENT(5,1)\|PYROXENE RICH MINERAL(5,1)\|RAW SLURRY(5,1)\|REACTED SLURRY RISE(5,1)\|RESIDUAL VAPOR(5,1)\|SCRUBBING ZONE(5,1)\|SILICATE CONVERSION(5,1)\|SLURRY REACTION(5,1)\|TRANSPORTING ORE(5,1)\|FINAL PRODUCT SLURRY(4,4)\|ADJACENT FLOW PATH(4,2)\|BOTTOM ASH PULVERIZATION(4,2)\|LIMESTONE(4,2)\|RESIDUAL AMMONIA SCRUBBER DETAIL(4,2)\|WOLLASTONITE(4,2)\|ABUNDANCE(4,1)\|AGITATION EQUIPMENT(4,1)\|AMMONIA SALT(4,1)\|AMMONIA VAPOR FLOW(4,1)\|CARBONATE SILICA SLURRY(4,1)\|CENT NITROGEN(4,1)\|CLASSIFICATION(4,1)\|CLEAR SUPERNATANT(4,1)\|COLD SLURRY(4,1)\|CONTINENTAL LAND MASS(4,1)\|COUNTERCURRENT HEAT EXCHANGER(4,1)\|DIVALENT IRON(4,1)\|FLASH RECTIFYING VESSEL(4,1)\|GAS TONNE(4,1)\|HOT PRODUCT PIPELINE(4,1)\|INSOLUBLE MAGNESIUM HYDROXIDE(4,1)\|KEEPING UP(4,1)\|MAGNESIUM CARBONATE EXTRACTION(4,1)\|MAGNESIUM ION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|OXIDE REACTION(4,1)\|PIPE REACTOR(4,1)\|PIPELINE HEAT EXCHANGER(4,1)\|PIPELINE REACTOR CONFIGURATION(4,1)\|PREPROCESSING(4,1)\|PUMPING CAPACITY(4,1)\|RECUPERATIVE HEAT EXCHANGER(4,1)\|SLURRY COOLING(4,1)\|SLURRY UPFLOW RATE(4,1)\|STRATEGIC LOCATION(4,1)\|WT SLURRY(4,1)\|REACTION CHAMBER(3,4)\|SOX(3,3)\|INSULATION(3,2)\|LIQUID AMMONIA RECOVERY(3,2)\|SHELL(3,2)\|SINGLE INTEGRATED(3,2)\|AIR PREHEATING(3,1)\|AMMONIA ABSORBER(3,1)\|AMMONIA GAS PIPE DIAMETER(3,1)\|AMMONIA METAL SILICATE SLURRY(3,1)\|AMMONIA RICH SOLUTION(3,1)\|AMMONIUM CARBONATE COMPOUND(3,1)\|ANNULUS(3,1)\|ARRIVAL PRESSURE(3,1)\|BAYSWATER POWER STATION(3,1)\|BICARBONATE(3,1)\|BIOMASS(3,1)\|BUOYANCY(3,1)\|CARBAMATE(3,1)\|CARBON DIOXIDE ABSORPTION ZONE(3,1)\|CHILLED GROUND METAL SILICATE(3,1)\|CHILLED SOLUTION(3,1)\|CIRCULATION NATURAL RATE(3,1)\|CLADDING(3,1)\|CLEAN FLUE GAS(3,1)\|CONCENTRIC INNER PIPE(3,1)\|COOL GAS(3,1)\|CRUSHING(3,1)\|DESTRUCTION(3,1)\|DISCHARGE END(3,1)\|DOLIME(3,1)\|DOMINANT METAL(3,1)\|DOWNSTREAM GAS(3,1)\|EARTH METAL SILICATE ROCK(3,1)\|ELECTROSTATIC PRECIPITATOR(3,1)\|GAS LIQUID SEPARATOR(3,1)\|GEOLOGICAL CONDITION PERMIT(3,1)\|HARMFUL CARBON DIOXIDE GAS(3,1)\|HEAT BALANCE FIGURE(3,1)\|HEAT CONSERVATION(3,1)\|INDICATIVE MASS(3,1)\|	(EP2134449)\|1. A carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor (52,70) that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|2. A process in accordance with claim 1, wherein in step (i), pressurised liquid ammonia is charged into the metal silicate slurry in such a manner that the liquid ammonia partially flashes to a vapour to produce the ammonia/water/metal silicate slurry.\|3. A process in accordance with claim 1 or claim 2, wherein the step of scrubbing the gas stream comprises exposing the carbon dioxide-containing gas stream into a spray of the slurry.\|4. A process in accordance with any one of the preceding claims, wherein the step of controlling the reactor comprises elevating at least one of a pressure and temperature of the reactor (52, 70) so as to enhance the reaction between the carbon dioxide and the metal silicate.\|5. A process in accordance with any one of the preceding claims, wherein the reactor (52,70) is a pipeline (52) comprising multiple flow paths such that the reaction takes place along the length of one of the flow paths while another of the flow paths is utilised to supply the metal silicate slurry to the first stage; optionally comprising the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\|6. A process in accordance with any one of claims 1 to 4, wherein the reactor is an underground chamber (70) located at a depth that provides sufficient pressure to enhance the reaction between the carbon dioxide and the metal silicate.\|7. A process in accordance with any one of the preceding claims, comprising the further step of recovering ammonia resulting from the reaction stage (iii) and recycling it to the first stage; optionally comprising the further step of introducing an alkali to the metal carbonate product resulting from the reaction stage (iii) prior to carrying out the ammonia recovery step.\|8. A process in accordance with claim 7, wherein the ammonia is recovered as both a liquid and a gas, with the liquid being converted partially to a vapour for recycling in the first stage and the gas being extracted, condensed and mixed with the metal silicate before it is supplied in the first stage; optionally wherein the step of recovering the ammonia is effected in a recovery vessel (54) which is pressurised to facilitate the recovery of ammonia in liquid form.\|9. A process in accordance with any one of the preceding claims, comprising the further step of grinding a metal silicate rock to produce the metal silicate slurry.\|10. A process in accordance with any one of the preceding claims, wherein the metal silicate is a magnesium silicate.\|11. A process in accordance with any one of the preceding claims, wherein the slurry of metal silicate rock is chilled prior to passing the slurry to the second stage.\|12. A process in accordance with any one of the preceding claims, wherein:\| - prior to passing the ammonia to the first stage, a pressurised liquid ammonia is allowed to expand in an evaporator stage so as to provide a cooling effect in the evaporator stage; and\| - the resultant ammonia/water/metal silicate slurry produced in the first stage is passed through the evaporator stage so as to chill the ammonia/water/metal silicate slurry.\|13. A process in accordance with claim 12, comprising the further step of withdrawing the chilled slurry and passing it to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammonia/water/metal silicate slurry to thereby absorb the carbon dioxide into the slurry.\|14. A process in accordance with claim 13, comprising the further step of recirculating the reactive slurry containing absorbed carbon dioxide through the evaporator stage and then to the scrubbing stage.\|15. A process in accordance with any one of claims 12 to 14, wherein the evaporator stage is carried out in an evaporation chamber (82).\|16. A system for (10) sequestering carbon dioxide from a gas stream, the system for comprising:\| (a) a first apparatus (28,30) for removing the carbon dioxide from the gas stream and for absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and\| (b) a reactor (52,70) for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|17. A system in accordance with claim 16, wherein the first apparatus comprises an ammonia absorption chiller (82) arranged to mix the metal silicate with ammonia to produce the ammoniated slurry.\|18. A system in accordance with claim 16 or claim 17, wherein\| (a) the reactor is a pipeline (52) comprising multiple flow paths and wherein the reaction takes place along the length of one of the flow paths; or\| (b) the reactor is a chamber (70), located in use underground; optionally wherein the chamber is located at a depth that provides sufficient pressure to enhance the reaction between the carbon dioxide and the metal silicate.\|19. A system in accordance with claim 18, wherein:\| - in the case of (a) the pipeline (52) comprises:\| a first flow path that (44) carries the metal silicate slurry to the first apparatus (28,30); and\| a second flow path (52) that carries from the first apparatus (28,30) the reactive slurry comprising carbon dioxide absorbed in an ammonia/water/metal silicate slurry, the second flow path being controlled so as to encourage the carbon dioxide to react with the metal silicate and produce a metal carbonate;- in the case of (b) the reactive slurry that comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry is provided to the chamber (70) for a sufficient period to enable it to react.\|20. A system in accordance with any one of claims 16 to 19, wherein the metal silicate comprises a magnesium silicate.\|21. A system in accordance with any one of claims 16 to 20, further comprising an ammonia absorption recovery vessel arranged to recover ammonia contained in the metal carbonate product.	(EP2134449)\|Technical Field\|[0001] This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|Background to the Invention\|[0002] There is increased focus on reducing carbon dioxide emissions to the atmosphere, to help minimise the effects of global warming. Carbon dioxide sinks exist naturally, with the main naturally occurring sink being the ocean. Plants are also an effective form of carbon dioxide sink and use photosynthesis to remove carbon from the atmosphere by incorporating it into biomass. However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\|[0003] The major source of harmful carbon dioxide gases are large fossil fuel power stations which, when fuelled by black coal, on average typically output around 0.8 to one tonne of the gas for each MegaWatt-hour (MWh) of electricity they generate. For example, a large power station such as the 2,640 MW Bayswater in the Hunter Valley of New South Wales, Australia, in generating 20 million MWh of electricity in a year, would also output 18 million tonnes of carbon dioxide. It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations. It would also be advantageous if a system and method were provided for the disposition of the gas to be independently audited.\|[0004] Known methods of sequestering carbon dioxide are described in WO 2006/008242, WO 200=4/0940=t3, WO 2005/108297 and WO 200=4/0987=40. WO 2006/022885 describes a method of ultra-cleaning a combustion gas, followed by capture and regeneration of carbon dioxide. The application does not describe a process in which a reaction between a metal silicate is controlled to produce a metal carbonate. There is also no disclosure of absorbing carbon dioxide in an ammoniated slurry that contains a metal silicate dispersed through it.\|Summary of the Invention\|[0005] In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|[0006] It should be noted that the terminology "gas stream containing carbon dioxide" does not mean that the stream contains only carbon dioxide, and may contain other off gases.\|[0007] In an embodiment of step (i), pressurised liquid ammonia is charged into the metal silicate slurry in such a manner that the liquid ammonia partially flashes to a vapour to produce the ammonia/metal silicate slurry.\|[0008] An embodiment of step (ii) may comprise exposing the carbon dioxide-containing gas stream to a spray of the slurry.\|[0009] An embodiment of step (iii) may comprise elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\|[0010] In an embodiment, the reactor is a pipeline. The pipeline preferably comprises multiple flow paths. In an embodiment, the reaction takes place along the length of one of the flow paths. Another of the flow paths may be utilised to supply the metal silicate slurry to the first stage.\|[0011] In an embodiment, the method comprises the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\|[0012] In an embodiment, the reactor is a chamber located in use underground. Preferably, the chamber is located at a depth that provides sufficient pressure to enhance the reaction between the carbon dioxide and the metal silicate. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0013] In an embodiment, the method may also comprise the step of recovering ammonia resulting from the reaction stage (iii) and recycling it to the first stage. In an embodiment, an alkali is added to the final product prior to performing the step of recovering ammonia. The alkali may be power station fly ash or pulverised bottom ash obtained by filtering or otherwise cleaning the carbon dioxide-containing flue gas stream. The ammonia may be recovered as both a liquid and a gas, with the liquid being converted partially to a vapour for recycling in the first stage and the gas being extracted, condensed and mixed with the metal silicate before it is supplied in the first stage.\|[0014] In an embodiment, the step of recovering the ammonia is effected in a recovery vessel which is pressurised to facilitate the recovery of ammonia in liquid form at ambient temperatures. In an embodiment, the recovery vessel is in use located at a depth sufficient for achieving the pressure to recover the ammonia in liquid form. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0015] In an embodiment the process comprises the further step of grinding a metal silicate rock to produce the metal silicate slurry. The metal silicate slurry may comprise 30 to 60% finely ground solids by weight. In an embodiment, the metal silicate is a magnesium-rich silicate mineral. The magnesium rich silicate may be comprised of a serpentine- and/or olivine- and/or pyroxene-rich mineral.\|[0016] In accordance with a second aspect, the present invention provides a system for sequestering carbon dioxide from a gas stream, the system comprising:\| (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and\| (b) a reactor for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|[0017] In an embodiment, the first apparatus comprises an ammonia absorption chiller arranged to (a) chill the metal silicate slurry and (b) mix the chilled slurry with ammonia to produce the ammoniated slurry. In an embodiment step (a) is carried out prior to step (b).\|[0018] The reactor may comprise the pipeline as set forth in the first aspect. In an alternative embodiment, the reactor may comprise the chamber as set forth in the first aspect. The metal silicate may comprise a magnesium rich silicate as set forth in the first aspect. In an embodiment, the system comprises a recovery vessel arranged to recover ammonia contained in the metal carbonate product.\|[0019] In accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the carbon dioxide to react with the metal silicate and produce a metal carbonate.\|[0020] In accordance with a fourth aspect of the present invention there is provided a method for causing a slurry, comprising carbon dioxide absorbed in an ammonia/water/metal silicate slurry, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the carbon dioxide and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|[0021] In an embodiment, the slurry provided to the chamber is the reactive slurry produced in the process as set forth in the first aspect. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0022] In an embodiment, the method comprises the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber. In an embodiment, the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.\|[0023] In accordance with a fifth aspect there is provided a power station utilising a carbon sequestration system in accordance with the second aspect, the system arranged to sequester carbon dioxide from flue gas emitted by the power station.\|[0024] In accordance with a sixth aspect, in an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, there is provided the steps of: (i) prior to passing ammonia to the absorption process, allowing the ammonia in pressurised liquid form to expand in an evaporator stage so as to provide a cooling effect in that stage; and (ii) passing the water/metal silicate slurry through the evaporator stage so as to chill said water/metal silicate slurry, prior to mixing it with the ammonia in the ammonia absorber process.\|[0025] In an embodiment, the process comprises the further step of providing the ammoniated slurry to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammonia/water/metal silicate slurry to thereby absorb the carbon dioxide into a reactive slurry.\|[0026] In an embodiment, the process comprises the further step of passing reactive slurry which is to be re-circulated through the scrubbing chamber through the evaporator stage prior to re-circulation. The evaporator stage may be implemented in an evaporator chamber. The scrubbing stage may be implemented in the first apparatus, as set forth in the second aspect.\|[0027] In accordance with a seventh aspect of the present invention there is provided an ammonia absorption chamber arranged to implement the process as set forth in the sixth aspect.\|[0028] In accordance with an eighth aspect of the present invention there is provided a method of extracting a target metal from a metal silicate comprising the step of mixing the metal silicate with a solution that comprises ammonia and ammonium salt, whereby the ammonia reacts with the metal silicate to cause the target metal to dissolve into the solution.\|[0029] In an embodiment the method comprises the further step of grinding the metal silicate and forming it into a slurry prior to mixing the metal silicate with the solution.\|[0030] In an embodiment the mixing takes place in an ammonia absorption chamber.\|[0031] In an embodiment the metal silicate is a magnesium-rich silicate.\|[0032] In an embodiment the magnesium-rich silicate is a serpentine and/or olivine and/or pyroxene silicate metal.\|[0033] In an embodiment the ammonium in solution comprises ammonium carbonate.\|[0034] In an embodiment the target metal dissolves into the solution and then precipitates as a metal carbonate to be removed for recovery.\|[0035] In an embodiment the target metal is one or more of magnesium, iron, copper and nickel. The dominant metal within the metal silicate may comprise magnesium.\|[0036] In a ninth aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a chilled slurry of a metal silicate rock with ammonia so as to produce a chilled ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the chilled solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|Brief Description of the Drawings\|[0037] An embodiment of the present invention will now be described, by way of example only, with reference to the accompanying drawings, in which:\| Fig. 1 is a schematic of a carbon dioxide sequestration system according to an embodiment of the present invention;\| Fig. 1A is a further schematic of a carbon dioxide sequestration system according to an embodiment of the present invention with additional detail of the Residual Ammonia scrubber, Ammonia absorber, and CO2 absorber shown.\| Fig. 2 is a process flow diagram showing a method of sequestering carbon dioxide using the system of Fig. 1, in accordance with an embodiment of the present invention;\| Fig. 3 is a schematic of a pressure exchange apparatus utilised by the carbon dioxide sequestration system of Fig. 1, in accordance with an embodiment of the present invention;\| Fig. 4 is a schematic of a heat exchange apparatus utilised by the carbon dioxide sequestration system of Fig. 1, in accordance with an embodiment of the present invention; and\| Fig. 5 is a schematic of a carbon dioxide sequestration system, according to an alternative embodiment of the present invention.\| Fig. 5A is a further schematic of a carbon dioxide sequestration system, according to an alternative embodiment of the present invention with additional detail of the Residual Ammonia scrubber, Ammonia absorber, and CO2 absorber shown.\|Detailed Description of an Embodiment\|[0038] In the following description, an embodiment of the present invention is described in the context of a system, apparatus and method for the capture and sequestration of carbon dioxide contained within flue gases emitted by a fossil fuel-fired power station. However, it is to be understood that the system, apparatus and method could equally be utilised for the permanent sequestration of carbon dioxide from any source and is not limited to the particular arrangement described herein.\|[0039] With reference to Fig. 1 there is shown a flow diagram of a system 10 for performing a carbon dioxide (CO2) sequestration process from a gas feed stream containing carbon dioxide outputted from a power station, in accordance with an embodiment of the present invention. With additional reference to Fig. 2, the system is arranged to perform the process 100 of (i) in a first stage, mixing a slurry of chilled ground metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the ammonia/water/metal silicate solution to thereby absorb the carbon dioxide into a reactive solution; and (iii) passing the reactive solution through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate and by-product silica (stage three).\|[0040] In an embodiment, the slurry of ground metal silicate rock is chilled by circulating the slurry through a vessel in which ammonia evaporates. In an embodiment another stage is carried out prior to stage (ii), namely contacting flue gases in a vessel in a counter-current, staged manner so that residual ammonia in the flue gases is scrubbed from these gases to levels low enough to allow their final discharge in the atmosphere.\|[0041] In the illustrated embodiment the three stages are performed successively, with the first two stages occurring within a first apparatus 20 in the form of two separate reaction chambers, namely an absorption chamber 28 and a scrubbing chamber 30, and the last stage occurring within a reactor in the form of a pipeline 52 which may, for example, connect the mine site to the power plant. As will be described in detail in subsequent paragraphs of the specification, the reactor may alternatively take the form of an underground chamber (see Fig. 5) excavated at a sufficient depth to facilitate the conditions for the carbonation reactions to take place.\|[0042] The carbon dioxide sequestration process utilised in embodiments of the present invention is based on mineral carbonation. Mineral carbonation is a reaction between a metal-oxide bearing material and carbon dioxide. The metal-oxide bearing material may for example be alkaline-earth metals. Advantageously, the process 100 does not require the source of carbon dioxide to be particularly pure. In mineral carbonation, carbon dioxide reacts with the metal oxide bearing material to generate insoluble carbonates, that is to say:\| MO + CO2 → MCO3 + heat (1)\|which is an exothermic reaction, occurring more rapidly at elevated temperature, typically above 200°C. Certain chemicals may serve to increase the rate at which this reaction proceeds without being consumed themselves, i.e. they serve as catalysts. The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|[0043] The exact nature of the insoluble carbonates formed by the reaction depends on the metal-oxide bearing material. Suitable materials may be naturally occurring alkaline-earth metal-rich silicate rocks which contain mineral constituents such as serpentinite (Mg3Si2O5(OH)4), olivine (Mg2SiO4), orthopyroxene (MgSiO3), talc (Mg3Si4O10(OH)2) and wollastonite (CaSiO3). In practice, the element Iron (Fe) may substitute for some of the Magnesium (Mg) or Calcium (Ca). Other suitable materials include alkaline industry residues such as slag from steel production, the ash (both fly and bottom) from pulverised coal-fired boilers, the ash remaining from the combustion of paper recycling residues (de-inking ash), and cement. The amount of heat generated in the reaction will depend on the specific metal and on the mineral containing the metal oxide as can be seen below in the case of three natural silicates (heat values are given per unit mole of CO2 and at standard conditions (25°C and 0.1 MPa):\| Olivine\| Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 + 89 kJ mol-1 CO2 (2a)\| Serpentine\| Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol-1 CO2 (2b)\| Wollastonite\| CaSiO3 + CO2 → CaCO3 + SiO2 + 90 kJ mol-1 CO2 (2c)\|[0044] A preferred silicate rock (because of its greater abundance in continental land masses) comprises the mineral serpentine, Mg3Si2O5(OH)4, All of these minerals may be pre-treated to increase the surface area of rock that can come into direct contact with the carbon dioxide. In an embodiment, the pre-treatment involves crushing, grinding and/or milling of the mineral, as well as some mechanical classification and separation. Typically, these minerals would be wet-milled in ball mills or equivalent to form a finely ground metal silicate slurry (hereafter 'silicate slurry') 36 wherein 90% of the mineral matter was finer than 40 microns. However, the extent of the pre-treatment is dependent upon the source and type of mineral(s) being used in the process.\|[0045] With specific reference to Fig. 1, the carbon dioxide sequestration system 10 will now be described in detail. The system 10 receives a raw flue gas mixture feed stream 32 that has been generated and subsequently emitted by a power station (not shown). In the embodiment described herein, the raw flue gas mixture 32 is passed though a filter 34 to remove particulate matter. Suitable filters may include fabric filters, electrostatic precipitators and the like. Cleaning the raw flue gas mixture 32 serves to minimise both the maintenance costs in downstream gas-handling equipment and the concentrations of particulates in flue gases ultimately discharged to the atmosphere. It will be understood, however, that while desirable for process reasons, it is not essential that the raw flue gas mixture 32 be cleaned of particulates before it enters the scrubbing chamber 30.\|[0046] To maximise heat recovery in the system 10, the filtered flue gas mixture is then passed through a heat exchange apparatus in the form of a heat exchanger 34 so that the sensible heat of the filtered flue gas mixture (typically emitted at a temperature of around 135°C) is exchanged with the cooler gasses being expelled from the scrubbing chamber 30 of the first apparatus 20 and the filtered flue gas mixture is cooled to its water-vapour saturation temperature (i.e. to about 50°C). Suitable heat exchangers may include, for example, recuperative-type heat exchangers, such as the Ljungstrom rotary design as used for air pre-heating in power stations.\|[0047] As mentioned in preceding paragraphs, the carbon dioxide sequestration system 10 receives a source of silicate slurry 36. According to the embodiment described herein, the silicate slurry source is located near or at the mine site from which the silicate rocks are sourced. As previously described, the silicate mineral sourced from the mine site is finely ground (preferably by wet-milling in ball mills or equivalent to form the slurry) wherein 90% of the mineral matter is finer than 40 microns. The silicate slurry 36 is subsequently passed through a first pressure-exchange apparatus 38. To minimise power consumption, the pressure of the silicate slurry 36 may be increased by exchanging pressure with the final metal carbonate/silica product (hereafter `final product'), typically to a pressure of approximately 10 Bar. In addition, to minimize heat losses from the system 10 (and to ensure that the final product is cooled to a suitable temperature before it is emplaced in its final permanent repository), the silicate slurry 36 passes counter-currently through a second heat exchanger 40 to absorb the surplus sensible heat contained in the final product. At a second pressure-exchange apparatus 42, the pressure of the silicate slurry 36 is further increased, this time to a substantially higher level (typically 100 Bar). Again, this boost in pressure is achieved by exchanging pressure, but this time with the carbonate/silica slurry prior to it undergoing treatment in the ammonia gas recovery vessel 54 (as will be described in detail in subsequent paragraphs).\|[0048] A pipeline 44 connects the first apparatus 20 to the mine site and is used to transport the silicate slurry 36 used in the sequestration process 100. As will be described in more detail in subsequent paragraphs, an alternate path 52 in the pipeline 44, in this embodiment, also serves to act as a controlled reactor in which the metal carbonate reaction largely takes place. At or near to the power station site, the silicate slurry 36 is passed counter-currently through a third heat exchanger 46 and a third pressure-exchange apparatus 48, where the silicate slurry 36 is cooled and reduced in pressure by exchange with the reactive slurry discharged from the first apparatus 20, before being fed directly into the evaporator vessel 82, where ammonia which has passed through the expansion valve 29 and is now at a very low temperature, cools the silicate slurry to near freezing. To ensure that the silicate slurry 36 is not actually frozen, a portion of this slurry is circulated through the evaporator vessel. The chilled silicate slurry passes downwards through a vessel, the residual ammonia scrubber, in such a way that cleaned and cooled flue gases that have been stripped of most of their carbon dioxide content, pass upwards from below. There may be as many as six counter-current contacting stages, such that the cleaned, largely carbon dioxide-free flue gases may leave the system with less than one part per million of ammonia.\|[0049] The silicate slurry, now charged with any ammonia arriving in flue gases from below, enters the ammonia absorber 28, where it absorbs into solution all of the ammonia that is recovered in the ammonia recovery vessel 54 so as to produce a ammonia/water/metal silicate slurry.\|[0050] The ammonia is recycled from the ammonia gas recovery stage of the process (described in subsequent paragraphs), with additional quantities required only to make up for losses, which should be small. Recovered liquid ammonia (which may contain small amounts of water) is supplied to the absorption chamber 28 by way of a pipeline 60, under pressure. In a preferred embodiment, pressurised liquid ammonia passes through the pressure reduction valve 29, which reduces its pressure to near atmospheric, at which pressure it discharges into a vessel, the evaporator chamber 82, prior to entering the absorption chamber 28. A portion of the ammonia will flash to vapour upon entering the evaporator chamber 82. The ammonia, in vaporising, absorbs substantial quantities of latent heat which is withdrawn from the slurries circulating through banks of tubes in the evaporator chamber 82, thereby chilling them to near freezing. In the embodiment shown in Fig. 1, the heat absorbed as the ammonia vaporises is drawn from the silicate slurry used as the residual carbon dioxide scrubbing medium in the residual ammonia scrubbing chamber. This is to ensure that the scrubbing medium last in contact with the cooled, filtered flue gases is the most chilled.\|[0051] The vaporised ammonia flows from the evaporator chamber 82 directly into the ammonia absorption chamber 28, wherein it is rapidly absorbed into the deluging spray of circulating silicate slurry 36 after this has passed downwards through the several stages of the residual carbon dioxide scrubber, to produce the ammonia/water/metal slurry used as the circulating scrubbing medium for the carbon dioxide scrubbing chamber 30. When the ammonia is absorbed in the silicate slurry 36 a substantial quantity of heat is liberated: the heat of solution of ammonia gas in water. Much of this heat is removed as the slurry circulates through the heat exchanger 84. As illustrated, the heat exchanger 84 and cooling tower also serve to remove much of the excess low-grade heat generated from the absorption of the ammonia in the silicate slurry.\|[0052] The cooled filtered flue gas mixture passing through the heat exchanger 34 enters the scrubbing chamber 30 where the gas mixture passes upwards through deluging sprays of absorbent slurry, the absorbent slurry having been drawn from the ammonia absorption chamber 28 and discharged into the head space of the scrubbing chamber 30. When carbon dioxide is absorbed in the ammonia/water/metal silicate slurry, a further substantial quantity of heat is liberated, as carbon dioxide and ammonia form in solution a series of ammonium carbonate compounds. With sufficient ammonia supplied to the absorption chamber 28 to achieve 90 per cent capture of carbon dioxide, the tendency will be to form the bicarbonate NH4HCO3 in preference to the normal carbonate (NH4)2CO3 and the carbamate, NH2COONH4, which will also be present in smaller quantities, perhaps along with some urea, CO(NHZ)2. The system 10 is configured such that the coldest slurry will be the last to contact the stripped (of carbon dioxide) flue gas mixture, in such a way that ammonia slip (losses in final flue gases to the atmosphere) are essentially eliminated. In the embodiment shown in Fig. 1, the scrubbing chamber 30 is shown as being constructed separately to the absorption chamber 28. Suitable scrubbing chambers may be generally similar to the type used for flue gas desulphurisation.\|[0053] As previously described, the sensible heat is removed from the filtered flue gas mixture in the first heat exchanger 34, cooling it to around 50°C, before entering the scrubbing chamber 30. The clean flue gases exiting the scrubbing chamber 30 typically comprise around 95 per cent nitrogen and inerts by volume. The balance comprises some oxygen and around 1.5 per cent carbon dioxide, being the remnant quantity of this gas after some 90 per cent had been stripped out in the scrubbing chamber 30.\|[0054] The resultant product of this two-stage process is a reactive solution in the form of a metal silicate slurry in an aqueous phase that is itself primarily a solution of ammonium carbonates. A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor. On route to the mine site, at or near to the power station, the reactive slurry is pressurised at the third pressure-exchange apparatus 48 to a high pressure of around 120 Bar (above the critical pressure of ammonia) and also heated to close to the boiling point of water at the pressure in question. Heating is accomplished firstly by transferring heat from the incoming silicate slurry arriving from the mine at the heat exchanger 46, and also by injection of steam 54. Without being bound by theory, the inventor anticipates that, subject to the process design assumptions of Example 1 (see table below), around 600 tonnes per hour of steam would be required to raise the temperature of the reactive slurry by around 100°C, to say 225°C, at which temperature the carbonation reactions are likely to reach acceptable rates. Heat liberated from the reaction between carbon dioxide and the metal silicate in the reactive slurry, which is highly exothermic, is capable on its own of raising the reactive slurry temperature by around 75°C (under the assumptions made in respect of Example 1), to yield a final temperature of some 300°C by the time the reactive slurry reaches the vicinity of the mine site, or site of other final emplacement. This temperature rise would be obtained despite some losses along the length of the return pipeline 52, notwithstanding attempts to minimise such losses by cladding this pipeline 52 throughout its length by suitable insulation (lagging).\|[0055] In the return pipeline 52 of the pipe reactor, most if not all of the carbon dioxide present in the reactive slurry can react with the silicate minerals and convert to insoluble carbonate during approximately the few first hours of transit. Each hour may correspond to a 10 kilometre length of this pipeline. In practice, however, the power station and the mine site may be much more than this distance apart, thereby allowing more than adequate time for reactions to proceed essentially to completion resulting in the metal carbonate product that contained most if not all of the carbon dioxide originally scrubbed from the power station flue gases. A high concentration of ammonia is maintained in the slurry throughout its passage from the power station to the mine/quarry or other emplacement site.\|[0056] When the final product in the return pipeline 52 reaches the vicinity of the mine site, as described above, it is passed through the second pressure-exchange apparatus 42 to lower the pressure of the stream from perhaps as high as 120 Bar to around 15-20 Bar, before entering the ammonia gas recovery vessel 54. With the temperatures indicated on Fig. 1, all of the ammonia and some of the water flash to vapours (the water would boil, the ammonia being driven out of solution) as the final product enters the ammonia gas recovery vessel 54, a consequence of a drop in temperature of more than 100°C. As shown in Fig 1, the hot pressurised final product transfers its sensible heat to the contents of the ammonia gas recovery vessel 54. This heat input assists to maximise the system's efficiency, as stripping the ammonia from the product as a gas absorbs considerable heat energy. To minimize the waste products generated by the system 10, and prior to entering the pipeline 44 for delivery to the continuous reactor 22, silicate slurry from the mine site is fed and re-circulated in the residual ammonia absorber 56 where residual vapours from the ammonia gas recovery vessel 54 are passed. A gas phase stream exiting from the top of the ammonia gas recovery vessel 54 contains essentially all of the free ammonia, which along with some water vapour condenses out in a condenser 58 to form a liquid phase that is mostly ammonia. In an embodiment, the condenser 58 is cooled by circulating water from dry (e.g. radiator-type) cooling towers, fin fan coolers, or, because no fans are required, a natural-draft cooling tower (not shown) such as used for cooling in the power station. This recovered liquid ammonia, representing the bulk of the ammonia injected into the circulating slurry in the absorption chamber 28, flows under pressure (aided by pumps, not shown) through an overland ammonia pipeline 60 to the power station site.\|[0057] The final product carbonate slurry (containing nearly all of the carbon dioxide in the original power station flue gases but now sequestered as carbonates), leaves the bottom of the ammonia gas recovery vessel 54. The final product slurry is free of ammonia, and in a form suitable for permanent emplacement in mine voids or other purpose-built repositories (not shown). In these emplacements the solids can settle and consolidate, releasing much of the aqueous phase as a clear supernatant. This supernatant may be collected and re-used in the process, for example, to prepare the silicate slurry 36 and returned to the power station site, via pipeline 44.\|[0058] It should be noted that not all of the ammonia added in the first apparatus 20 can be recovered and returned to the process via the overland ammonia pipeline 60. Some ammonia may end up as ammonium salts: sulphites and sulphates, and as ammonium nitrites and nitrates, from SOx and NOx respectively in the raw flue gases. If the raw flue gas source is a flue gas generated by a typical fossil fuel-fired power station, and assuming use of modern low-NOx burners, losses of ammonia via these reactions should will be minor. Their presence in the final carbonate product slurry may furthermore, assist with rehabilitation of the final emplacements of the carbonate minerals. Figure 1A illustrates an alternative embodiment including a residual ammonia scrubber positioned within the scrubbing chamber 30.\|[0059] It may be desirable to reduce the losses of ammonia that would occur in this way. In an embodiment, this is achieved by dosing, or otherwise adding to the reacted slurry immediately prior to its entry into the ammonia recovery vessel 58, an appropriate quantity of slaked lime or other suitable alkali. A source of such alkali may be power station fly ash or pulverised bottom ash. The presence of limestone or dolomite in the original coal may render them suitable for this duty; in passing through the boilers much of this limestone or dolomite will be converted to alkalis suitable for ammonia recovery: quicklime or dolime (dolomite-lime), respectively.\|[0060] Should it arise that the content of limestone or dolomite in the coal fuel is inadequate for the duty (as is likely to be the case with most power station fly ashes), it is possible to dose the appropriate quantity of pulverised limestone or dolomite to the power station boilers (not shown). This dosing may be conducted at a location in the hot combustion gas path where the gas temperatures are in the range 800-1,000°C, i.e. sufficient to convert these minerals to the reactive oxide forms (lime, or dolime respectively). For example, this may occur upstream of the boiler's economiser. When the ammonia-recovery vessel is close to the power station, as it would be in the case of the underground chamber reactor embodiment (Fig. 5), it may be appropriate to add all of the power station fly ash to the final product slurry to maximise the regeneration of ammonia for re-use in the process. In this manner, both fly ash and the final product slurry from the carbon sequestration process may be handled and co-disposed of as a single stream. An anticipated advantage stemming from the presence of fly ash having pozzolanic properties (a tendency to set in the presence of alkalis and moisture) in the final product, will assist with the rehabilitation process, by encouraging the final product/fly ash mix to "set".\|[0061] With reference to Fig. 3, there is shown an arrangement for the pressure-exchange apparatus described above. At the end of the reaction process, the pressure of the final carbonate-rich product must be reduced from approximately 120 Bar to atmospheric pressure. As described above, this is undertaken in two stages: from 120 Bar down to around 15 Bar, a pressure suitable for operation of the ammonia recovery stage, then from 15 Bar down to atmospheric pressure. Instead of merely reducing pressure by throttling valves, thereby losing the energy embodied in this pressure, the energy this pressure represents may be conserved by transferring it to the extent possible, in two stages, to the silicate slurry. In Fig. 3, slurry A comprises the products of the reactions that occur as the ammoniated, carbonated silicate slurry flow through the pipeline 44 from the power station to the mine site; while slurry B represents silicate slurry from the mine. A consequence of pressure exchange in these two stages is that slurry A's pressure would fall from around 120 Bar to near ambient pressure, while that of slurry B would rise: in the first stage (working from right to left) to around 10 Bar, then to perhaps 100 Bar in the second stage.\|[0062] Another pressure-exchange apparatus is also utilised at the power station site. Here, using the terminology of Fig. 3, slurry A represents the hot silicate slurry arriving via the pipeline from the mine; while slurry B comprises slurry exiting the scrubbing chamber 30 (i.e. silicate slurry now charged with ammonia and carbon dioxide, but at close to ambient pressures). A consequence of pressure exchange in this stage is that slurry A's pressure would fall from its arrival pressure (this may be 120 Bar, a pressure that would be maintained by booster pumping stations at strategic locations (not shown) along the pipeline 44 to overcome friction losses), to near ambient pressure. This pressure may be transferred (exchanged) to the extent possible to slurry B, thereby minimising the amount of pumping energy required to raise the pressure of this slurry to the levels required, here assumed to be 120 Bar. Since slurry A at this point will be at well below 120 Bar, pressure-exchange between slurries A and B alone may not be capable of raising the pressure of slurry B to 120 Bar. Also, the volume of slurry B may exceed that of slurry A. This is because of the much higher contents of carbon dioxide and ammonia, and of water condensed out of the power station flue gases. In an embodiment, additional pumping capacity may be installed to boost slurry B pressures to those required for the pipeline 44, and to pressurise those (relatively small) quantities of slurry B that cannot be pressurised by pressure-exchange with slurry A. For this function, conventional high-pressure diaphragm pumps, such as the Geho pump manufactured by Weir Netherlands b.v., may be implemented. This pumping, together with the pumping energy required to maintain pressures along the length of the pipelines, account for a substantial proportion of the total mechanical energy input to the total process. Other suitable pressure exchange/pump-turbine sets may comprise centrifugal pumps and radial-type hydraulic turbines. As the pressures are relatively high, the type of centrifugal pump may be a multi-stage barrel-type pump.\|[0063] With reference to Fig. 4 there is shown a configuration for the heat exchanger arrangements 40 & 46, according to an embodiment of the present invention. As previously discussed, high temperatures are required to initiate and accelerate the carbon sequestration reactions: the conversion of silicates to carbonates. These reactions, being exothermic, yield additional heat that can and should be applied to assist with creating the conditions needed for these reactions to proceed most efficiently. As shown, the heat exchanger arrangement is in the form of a simple shell-and-tube heat exchanger, consisting of two concentric pipes: the inner forms the "tube", the outer, the "shell". An advantage with this arrangement is that the heat exchanger can be made as long as is required to effect the desired transfer of heat: if necessary, many hundreds of metres long. For heat exchanger 40 (i.e. the heat exchanger on the mine site side), heat energy is transferred between the final carbonate/silica product (i.e. slurry A), which is hot, and the silicate slurry (slurry B), which is cool. For heat exchanger 46 (i.e. the heat exchanger on the power station side), slurry A would be hot silicate slurry from the mine, while slurry B would be slurry exiting the scrubbing chamber 30 (i.e. now charged with ammonia and carbon dioxide, but at close to ambient temperatures).\|[0064] Turning now to Fig. 5, there is shown an alternative system 200 for performing carbon dioxide sequestration which utilises (where geological conditions permit) an underground chamber as the reactor, as opposed to a pipeline reactor as illustrated in Fig. 1. In this embodiment, the reactor is in the form of a chamber 70 excavated from bedrock at a depth sufficient to allow the conditions for the core carbonation reactions to be generated entirely or partly by static head alone (e.g. 120 Bar for the carbonation reactions and 20 Bar for the recovery of ammonia gas from the reaction products). A chamber 70 excavated at a depth of approximately 1,000 meters and having a volume of 150,000 cubic meters, sufficient to allow for a 24 hours detention time for the contents, may be envisaged for holding the reactive slurry output from a system 200 fitted to an efficient 1,000MWe coal-fired power station. In practice a smaller chamber may suffice, should it arise that the reactions are essentially completed in less time.\|[0065] The silicate slurry 36 may be prepared either at the serpentine mine site and pumped overland to the power station site, or, the mineral could be railed, trucked or otherwise suitably transported to the power station site, and prepared there. Were the former course of action adopted, pipeline arrangements 44 would be considerably simpler than for the pipeline reactor embodiment described above with reference to Fig. 1. Specifically, the silicate slurry 36 would not be required to collect and transport heat and pressure energy from the mine site to the power station site, nor to host any residual ammonia. The pipeline 44 would simply be utilised for ore transport; whether it was transported as a lump product by rail or as slurry by pipeline would be determined mainly by economic considerations. It will be appreciated that in this embodiment, silicate slurry density could be substantially higher (e.g. 60 per cent solids), thereby reducing the volumes of silicate slurry required to be pumped, and allowing a lower pipeline velocity because of the reduced tendency for the solids in denser slurries to segregate and silt up the pipeline 44. Also, arrangements for conserving heat and pressure are much simpler than they would need to be for the pipeline reactor alternative.\|[0066] In Fig. 5, an injection pump 72 is utilised to drive the circulation of the reactive slurry from the scrubbing chamber 40, through a plurality of counter-current heat exchangers 74, 76, underground reactor 70 and ammonia gas recovery vessel 78 (flash/rectifying vessel) and back to the surface. It is envisaged that a formation of bubbles of ammonia gas may occur as the reacted slurry rises from the underground reactor 70 (a rise accompanied by a loss of static head, hence of pressure), thereby reducing the bulk density of the reacted slurry rising from the reactor. It follows that the required circulation could be achieved by entirely natural means: after the injection pump 72 has achieved the circulation necessary for the reaction to proceed, it may be taken off line. The design of injection pump 72 may be such that it could run backwards, that is to generate power, should the natural rate of circulation created by the buoyancy effect of ammonia bubbles forming in the reactor outlet pipe 80 be sufficiently strong.\|[0067] Heat exchangers 74, 76 are shown in schematic form at two locations on Fig. 5. In practice, the heat exchangers 74, 76 could be long, shell-and-tube designs, as shown in Fig. 4: they would span most of the vertical distance from the scrubbing chamber 40 down to the underground chamber 70. This is to say, whereas two separate pipelines are implied in Fig. 5, in practice, for most of their length they would be concentric: the annulus formed between the outer and concentric inner pipe would transport the hot reaction products, while the inner pipe would transport the products heading downward to the Reaction chamber. It will be understood by persons skilled in the art that this selection may be reversed.\|[0068] In contrast to the pipeline reactor configuration shown in Fig. 1, heating of the reactive slurry is accomplished by exchanging heat from the hot reaction products rising first from the ammonia gas recovery vessel 78, and as the raw slurry descended further, from hot slurry rising from the underground chamber 70. While some supplementary heat may be required, the heat generated by Equation 2(b) would be conserved, and available to heat raw reactive slurry.\|[0069] The design of the underground chamber 70 may be optimised to achieve some plug-flow characteristics. In an embodiment, the chamber 70 may have a high length-to-diameter ratio and be vertically aligned. In this manner, the incoming reactive slurry, being cooler hence slightly denser than the average contents of the reactive chamber 70, would tend to stratify at lower levels, displacing hotter slurry upwards. In an embodiment, the underground chamber 70 may be subdivided into two or more vertically stacked sub-chambers.\|[0070] There should be no requirement for separate agitation equipment in the reaction chamber to maintain the solids in suspension. As shown in Fig. 5, incoming reactive slurry enters the vessel close to its base, and it is envisaged that settling rates will be small relative to overall slurry up-flow rates. If, however, large residence times are required, implying in turn large reactor volumes, a form of agitation may be implemented.\|[0071] As will readily be appreciated, heat losses from the underground chamber 70 and pipelines may be much smaller than they would be even from a lagged above-ground pipeline and may be further reduced by insulation surrounding the reactor, pipelines and all other underground process vessels. Whereas an overland pipeline represents a plug-flow reactor, ideal conditions for a relatively slow series of reactions as are involved in carbon sequestration are also obtained in the embodiment illustrated in Fig. 5.\|[0072] Also in Fig. 5, an alternative ammonia absorption recovery process is utilised. In this embodiment, as the final product slurry rises from the underground chamber 70, the static head it experiences may decrease. A consequence of this is that the boiling point temperature will fall, eventually below that of the slurry rising in the products pipeline, leading to the flashing of some of the water to steam, and the stripping of ammonia from solution. As ammonia comes out of the solution as a gas it will absorb latent heat from the final product slurry, partially cooling it; the temperature would tend to track the boiling point of water at the prevailing pressure. The bubbles of ammonia will reduce the average density of slurry in the hot products pipeline to below that in the incoming reactants pipeline, leading to a pressure differential in the system that would serve to drive the circulation of the reactant and product slurries from the CO2 Absorber 30 and through the underground chamber 70, heat exchangers and other items of process plant. As shown on Fig. 5, the ammonia recovery vessel 78 and other necessary plant and equipment for recovering ammonia from the product slurries are installed at a level (perhaps 150 metres below ground level) that facilitate the use of static head to maintain a pressure in the vessel 78 of around 15 Bar, i.e. high enough so that ammonia was a liquid at near-ambient temperatures.\|[0073] As for the pipeline reactor case, the ammonia will be discharged as a gas from the top of the vessel 78, however due to the circumstances outlined above, this vessel 78 could be much simpler in design and, in an embodiment, need be little more than a gas-liquid separator. While some additional heat energy may be required to recover essentially all of the ammonia as a gas, typically as steam, with the arrangements proposed the heat-energy burden of carbon sequestration could be greatly reduced.\|Examples\|[0074] Again with specific reference to Fig. 2, a non-limiting example process flow for carbon sequestration for the first system configuration 10 described herein (i.e. the system depicted in Fig. 1) will now be given, wherein for convenience, like parts to those shown in the foregoing embodiment have been numbered with like numerals.\|Example 1\|[0075] Table 1: Indicative mass and heat balance figures from 1.000 MWe of black coal-fired electricity generation plant.MaterialPer yearPer hourTotal CO2 generated:6.4 106 t800 tSilicate rock to absorb 90% of this CO2:145m 106 t1,800 tWater required to make 30% by wt slurry:33.6 106 t4,200Ammonia to conv. 90% of CO2 to (NH4)2CO3:4.45 106 t560 tHeat liberated (3.6 GJ/t CO2):2,800 GJTotal slurry with (NH4)2CO3:58 106 t7,2501Slurry density:1.3 t/m31.3 t/m3Slurry pipe dia. (both with 2 m/s velocity:1.0 m1.0 metresAmmonia pipe diameter, 2 m/s velocity0.4 m0.4 metresConc. of ammonia in Absorber aq. phase:12% (by wt)12%Ammonia lost due to SOx16,000 t2.0 tAmmonia lost due to NOx3,000 t0.37 tOther losses of ammonia:11,000 t1.38 tAmmonia make-up % of flow to Absorber:0.67%0.67%\|[0076] Table 1 provides a detailed mass and heat balance for a carbon dioxide sequestration process, assuming:\| 90 per cent carbon dioxide capture and sequestration from 1,000 MWe of black coal-fired electricity generation plant, which when operating in base-load mode might expect to generate annually 8,000 GWh of electricity;\| where on a dry ash-free basis, the coal is 81.3% by weight carbon and 0.65% sulphur (as S) and the flue gases contain 400 ppm NOx.\|[0077] The heat of formation of ammonium carbonate in solution from ammonia, water and carbon dioxide is around 2.0 GJ/tonne carbon dioxide equivalent, sufficient to heat the slurry by 75°C. Offsetting this is the heat absorbed when each tonne of ammonia is vaporised in the absorption zone, around 1.0 GJ/tonne ammonia. This is equivalent to around 1.8 GJ per tonne of carbon dioxide absorbed, sufficient to cool the slurry feed by around 60°C. It follows that there would be an overall temperature rise between the time the slurry feed enters the absorption zone and the time it enters the return pipeline 52, of around 15°C. In practice, it may be necessary to design the process so that the last slurry feed that the final largely carbon dioxide free flue gases is the coldest: less than 5°C.\|[0078] As well, the heat released when ammonium carbonate in solution reacts with the silicate rocks, roughly 1.45 GJ/tonne carbon dioxide absorbed, is sufficient to raise the temperature of the slurry feed by around 55°C. This occurs in the return pipeline 52.\|[0079] At the mine, the condensation of around 300 tonnes per hour of ammonia would release some 160 MWt of heat energy, which can be rejected to the environment via a cooling tower.\|[0080] An advantage of the carbon dioxide sequestration process 100 and systems 10, 20 according to embodiments of the present invention is that by selecting ammonia as a catalyst/promoter, a single integrated process can be provided for both capture and sequestration of carbon dioxide. In an embodiment, sequestration of the carbon dioxide takes place in a reactor, in the form of a return pathway 52 of a pipeline 44, which advantageously connects the power station (i.e. the source of carbon dioxide) to the source/destination of the absorbent material being used in the process. In an alternative embodiment, where geological conditions permit, the reactor may take the form of an underground chamber which advantageously facilitates the reaction without requiring pressure-exchange and head-recovery equipment required for the pipeline embodiment. Another advantage of the carbon dioxide sequestration process and systems is that the reaction kinetics may be improved by using ammonia. Therefore, by using ammonia and exploiting the heat generated by the exothermic reaction, the energy consumption of the process 100 can be kept to a minimum. As the reaction products are thermodynamically stable, carbon dioxide can be stored in a permanent stable solid form. Following from this, further advantages include lower operating and capital costs.\|[0081] Persons skilled in the art will appreciate that further advantages may arise from carrying out certain steps of the aforementioned embodiments in isolation. For example, the catalytic effect of a solution of ammonia with an ammonium salt (that may be ammonium carbonate formed by exposing an ammonia-rich solution to a gas stream containing carbon dioxide) in the carbon dioxide sequestration process can also be utilised for extracting metals (e.g. magnesium, iron, nickel, copper and other metals present in the silicate rock) from metal silicates, such as magnesium-rich metal silicates. In such an embodiment a solution comprising ammonia and ammonium may be mixed with a metal silicate (typically in slurry form) to allow the dissolution of magnesium ions by ammonia to recover the metal, in this embodiment a metal compound in the form of magnesium carbonate. The mixing may occur in an ammonia absorption chamber such as that previously described in connection with the preceding embodiments. Preferably the ammonia solution comprises concentrated ammonia in the presence of ammonia salts in solution, such as ammonium carbonate, to prevent the precipitation of magnesium hydroxide, hence allowing the dissolution of magnesium ions by ammonia to continue. A further advantage arising from this process is that after extraction of magnesium carbonate, other minerals (metals) present within the silicate rock are also amenable to recovery. The silicate rock may comprise mafic or ultra-mafic rocks (i.e. rocks with a high magnesium content).\|[0082] The catalytic effect of the ammonia follows from its tendency to form complexes (ammines) with certain metal ions including magnesium (Mg2+), divalent iron (Fe2+), copper (Cu2+) and nickel (Ni2+). The presence of ammonium salts notably the carbonate formed from the reaction between ammonia and carbon dioxide prevents precipitation of the otherwise insoluble magnesium hydroxide. Magnesium carbonate is however insoluble in such an environment, so a precipitate of this compound will form from the reaction between magnesium hydroxide and ammonium carbonate, to yield ammonium hydroxide and free ammonia in solution, the latter continuing to extract additional magnesium and other metals from the silicate rock through formation of ammine complexes until all such susceptible metals have been extracted.\|[0083] Subsequently, the ammonia is recovered from the solution by in the ammonia recovery vessel, a consequence being a progressive reduction in the concentration of free ammonia in the reactive slurry. This leads to destruction of the metal ammine complexes, but in a progressive manner, depending on the stability of the complexes, which stability in turn differs between metals. Those of magnesium are relatively weak (the reason most of the magnesium will have precipitated out as magnesium carbonate), so the first salt to be precipitated is further magnesium carbonate. As the concentration of ammonia in solution continues to fall, other metals can precipitate in sequence, allowing the opportunity of obtaining precipitates of each single metal in relatively pure form.\|[0084] Finally, it is to be appreciated that various alterations or additions may be made to the parts previously described without-departing from the spirit or ambit of the present invention as defined by the following claims. The process is not limited to having a single two-stage continuous reactor, or a single tube-like reactor, as the process may be arranged to utilise alternatively configured items of equipment as necessary to accommodate process variables, arising from different source materials, capital and operating costs. For example, in the exemplary embodiment previously described the plant design is based on the emission of 800 tonnes CO2/GWh generated from a state-of-the-art black coal-fired electricity generation plant. By comparison, the Bayswater Power Station and the Liddell Power Station, both in the Hunter Valley of New South Wales, Australia, able to generate 2,640 MWe and 2,040 MWe respectively, being older hence less efficient can be expected to emit between 850 and 900 tonnes CO2/GWh.\|[0085] Thus the concentration and rate of carbon dioxide emissions in the flue gas emitted by the power plant may vary such that the plant equipment design may be reconfigured to accommodate these variables. For example, alternative equipment can be configured for the various heat and pressure exchange stations. The carbon dioxide absorption zone and the scrubbing zone may be arranged in series in two separate vessels (rather than the nested configuration shown in Fig. 1). The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s). As well, the corresponding solids concentration in the slurry feed may be higher or lower than 30% solids by weight. It is possible that the metal silicate solution may comprise a blend of metal silicates, e.g. mixture of serpentines and olivines, even pyroxenes. The reaction kinetics may require heat to be removed from the reactive solution (rather than heat addition as described above). These factors will impact and alter the system pressures. There might be two or more pipelines for transporting the metal silicate solution and the reactive solution; because there are more pipelines additional heat exchangers and pressure-exchange apparatus may be used. The power station flue gas may include additional pre-processing steps including flue gas desulphurisation (FGD) and selective catalytic reduction (SCR) to reduce concentrations of SOx and NOx respectively hence losses of ammonia from the system. Furthermore, the availability of services, such as steam and cooling water may require different equipment arrangements.\|[0086] Any reference to prior art contained herein is not to be taken as an admission that the information is common general knowledge, unless otherwise indicated.\|[0087] In the claims which follow and in the preceding description of the invention, except where the context requires otherwise due to express language or necessary implication, the word "comprise" or variations such as "comprises" or "comprising" is used in an inclusive sense, i.e. to specify the presence of the stated features but not to preclude the presence or addition of further features in various embodiments of the invention.	(EP2134449)\|Technical Field\|[0001] This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|Background to the Invention\|[0002] There is increased focus on reducing carbon dioxide emissions to the atmosphere, to help minimise the effects of global warming. Carbon dioxide sinks exist naturally, with the main naturally occurring sink being the ocean. Plants are also an effective form of carbon dioxide sink and use photosynthesis to remove carbon from the atmosphere by incorporating it into biomass. However, these naturally occurring sinks are not capable of effectively keeping up with the vast quantities of carbon dioxide being produced in today's power-thirsty climate.\|[0003] The major source of harmful carbon dioxide gases are large fossil fuel power stations which, when fuelled by black coal, on average typically output around 0.8 to one tonne of the gas for each MegaWatt-hour (MWh) of electricity they generate. For example, a large power station such as the 2,640 MW Bayswater in the Hunter Valley of New South Wales, Australia, in generating 20 million MWh of electricity in a year, would also output 18 million tonnes of carbon dioxide. It would be advantageous if there was a system and method which was capable of capturing and permanently sequestering at least some of the carbon dioxide emitted from such power stations. It would also be advantageous if a system and method were provided for the disposition of the gas to be independently audited.\|[0004] Known methods of sequestering carbon dioxide are described in WO 2006/008242, WO 200=4/0940=t3, WO 2005/108297 and WO 200=4/0987=40. WO 2006/022885 describes a method of ultra-cleaning a combustion gas, followed by capture and regeneration of carbon dioxide. The application does not describe a process in which a reaction between a metal silicate is controlled to produce a metal carbonate. There is also no disclosure of absorbing carbon dioxide in an ammoniated slurry that contains a metal silicate dispersed through it.\|Summary of the Invention\|[0005] In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|[0006] It should be noted that the terminology "gas stream containing carbon dioxide" does not mean that the stream contains only carbon dioxide, and may contain other off gases.\|[0007] In an embodiment of step (i), pressurised liquid ammonia is charged into the metal silicate slurry in such a manner that the liquid ammonia partially flashes to a vapour to produce the ammonia/metal silicate slurry.\|[0008] An embodiment of step (ii) may comprise exposing the carbon dioxide-containing gas stream to a spray of the slurry.\|[0009] An embodiment of step (iii) may comprise elevating at least one of a pressure and temperature of the reactor so as to enhance the reaction between the carbon dioxide and the metal silicate.\|[0010] In an embodiment, the reactor is a pipeline. The pipeline preferably comprises multiple flow paths. In an embodiment, the reaction takes place along the length of one of the flow paths. Another of the flow paths may be utilised to supply the metal silicate slurry to the first stage.\|[0011] In an embodiment, the method comprises the further step of exchanging at least one of pressure and heat between the reactive slurry and the metal silicate slurry before and/or after the pipeline.\|[0012] In an embodiment, the reactor is a chamber located in use underground. Preferably, the chamber is located at a depth that provides sufficient pressure to enhance the reaction between the carbon dioxide and the metal silicate. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0013] In an embodiment, the method may also comprise the step of recovering ammonia resulting from the reaction stage (iii) and recycling it to the first stage. In an embodiment, an alkali is added to the final product prior to performing the step of recovering ammonia. The alkali may be power station fly ash or pulverised bottom ash obtained by filtering or otherwise cleaning the carbon dioxide-containing flue gas stream. The ammonia may be recovered as both a liquid and a gas, with the liquid being converted partially to a vapour for recycling in the first stage and the gas being extracted, condensed and mixed with the metal silicate before it is supplied in the first stage.\|[0014] In an embodiment, the step of recovering the ammonia is effected in a recovery vessel which is pressurised to facilitate the recovery of ammonia in liquid form at ambient temperatures. In an embodiment, the recovery vessel is in use located at a depth sufficient for achieving the pressure to recover the ammonia in liquid form. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0015] In an embodiment the process comprises the further step of grinding a metal silicate rock to produce the metal silicate slurry. The metal silicate slurry may comprise 30 to 60% finely ground solids by weight. In an embodiment, the metal silicate is a magnesium-rich silicate mineral. The magnesium rich silicate may be comprised of a serpentine- and/or olivine- and/or pyroxene-rich mineral.\|[0016] In accordance with a second aspect, the present invention provides a system for sequestering carbon dioxide from a gas stream, the system comprising:\| (a) a first apparatus for removing the carbon dioxide from the gas stream and absorbing it in an ammoniated slurry that contains a metal silicate dispersed through it; and\| (b) a reactor for receiving the slurry from (a), the reactor being controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|[0017] In an embodiment, the first apparatus comprises an ammonia absorption chiller arranged to (a) chill the metal silicate slurry and (b) mix the chilled slurry with ammonia to produce the ammoniated slurry. In an embodiment step (a) is carried out prior to step (b).\|[0018] The reactor may comprise the pipeline as set forth in the first aspect. In an alternative embodiment, the reactor may comprise the chamber as set forth in the first aspect. The metal silicate may comprise a magnesium rich silicate as set forth in the first aspect. In an embodiment, the system comprises a recovery vessel arranged to recover ammonia contained in the metal carbonate product.\|[0019] In accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the carbon dioxide to react with the metal silicate and produce a metal carbonate.\|[0020] In accordance with a fourth aspect of the present invention there is provided a method for causing a slurry, comprising carbon dioxide absorbed in an ammonia/water/metal silicate slurry, to react so as to produce a metal carbonate, the method comprising the steps of: positioning a chamber underground at a depth which is sufficient to provide a pressure in the chamber to enhance the reaction between the carbon dioxide and the metal silicate so as to produce the metal carbonate; and providing the slurry to the chamber for a sufficient period to enable it to react.\|[0021] In an embodiment, the slurry provided to the chamber is the reactive slurry produced in the process as set forth in the first aspect. In an embodiment the depth is sufficient for providing sufficient pressure by static head alone.\|[0022] In an embodiment, the method comprises the further step of exchanging heat from the product of the chamber with the slurry provided to the chamber. In an embodiment, the heat is exchanged in one or more heat exchanger units arranged in or at adjacent flow paths of the chamber product and the slurry.\|[0023] In accordance with a fifth aspect there is provided a power station utilising a carbon sequestration system in accordance with the second aspect, the system arranged to sequester carbon dioxide from flue gas emitted by the power station.\|[0024] In accordance with a sixth aspect, in an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, there is provided the steps of: (i) prior to passing ammonia to the absorption process, allowing the ammonia in pressurised liquid form to expand in an evaporator stage so as to provide a cooling effect in that stage; and (ii) passing the water/metal silicate slurry through the evaporator stage so as to chill said water/metal silicate slurry, prior to mixing it with the ammonia in the ammonia absorber process.\|[0025] In an embodiment, the process comprises the further step of providing the ammoniated slurry to a scrubbing stage, wherein a gas stream containing carbon dioxide is scrubbed with the chilled ammonia/water/metal silicate slurry to thereby absorb the carbon dioxide into a reactive slurry.\|[0026] In an embodiment, the process comprises the further step of passing reactive slurry which is to be re-circulated through the scrubbing chamber through the evaporator stage prior to re-circulation. The evaporator stage may be implemented in an evaporator chamber. The scrubbing stage may be implemented in the first apparatus, as set forth in the second aspect.\|[0027] In accordance with a seventh aspect of the present invention there is provided an ammonia absorption chamber arranged to implement the process as set forth in the sixth aspect.\|[0028] In accordance with an eighth aspect of the present invention there is provided a method of extracting a target metal from a metal silicate comprising the step of mixing the metal silicate with a solution that comprises ammonia and ammonium salt, whereby the ammonia reacts with the metal silicate to cause the target metal to dissolve into the solution.\|[0029] In an embodiment the method comprises the further step of grinding the metal silicate and forming it into a slurry prior to mixing the metal silicate with the solution.\|[0030] In an embodiment the mixing takes place in an ammonia absorption chamber.\|[0031] In an embodiment the metal silicate is a magnesium-rich silicate.\|[0032] In an embodiment the magnesium-rich silicate is a serpentine and/or olivine and/or pyroxene silicate metal.\|[0033] In an embodiment the ammonium in solution comprises ammonium carbonate.\|[0034] In an embodiment the target metal dissolves into the solution and then precipitates as a metal carbonate to be removed for recovery.\|[0035] In an embodiment the target metal is one or more of magnesium, iron, copper and nickel. The dominant metal within the metal silicate may comprise magnesium.\|[0036] In a ninth aspect the present invention provides a carbon dioxide sequestration process including the steps of:\| (i) in a first stage, mixing a chilled slurry of a metal silicate rock with ammonia so as to produce a chilled ammonia/water/metal silicate slurry;\| (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the chilled solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and\| (iii) in a third stage, passing the reactive slurry from (ii) through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate.\|Brief Description of the Drawings\|[0037] An embodiment of the present invention will now be described, by way of example only, with reference to the accompanying drawings, in which:\| Fig. 1 is a schematic of a carbon dioxide sequestration system according to an embodiment of the present invention;\| Fig. 1A is a further schematic of a carbon dioxide sequestration system according to an embodiment of the present invention with additional detail of the Residual Ammonia scrubber, Ammonia absorber, and CO2 absorber shown.\| Fig. 2 is a process flow diagram showing a method of sequestering carbon dioxide using the system of Fig. 1, in accordance with an embodiment of the present invention;\| Fig. 3 is a schematic of a pressure exchange apparatus utilised by the carbon dioxide sequestration system of Fig. 1, in accordance with an embodiment of the present invention;\| Fig. 4 is a schematic of a heat exchange apparatus utilised by the carbon dioxide sequestration system of Fig. 1, in accordance with an embodiment of the present invention; and\| Fig. 5 is a schematic of a carbon dioxide sequestration system, according to an alternative embodiment of the present invention.\| Fig. 5A is a further schematic of a carbon dioxide sequestration system, according to an alternative embodiment of the present invention with additional detail of the Residual Ammonia scrubber, Ammonia absorber, and CO2 absorber shown.\|Detailed Description of an Embodiment\|[0038] In the following description, an embodiment of the present invention is described in the context of a system, apparatus and method for the capture and sequestration of carbon dioxide contained within flue gases emitted by a fossil fuel-fired power station. However, it is to be understood that the system, apparatus and method could equally be utilised for the permanent sequestration of carbon dioxide from any source and is not limited to the particular arrangement described herein.\|[0039] With reference to Fig. 1 there is shown a flow diagram of a system 10 for performing a carbon dioxide (CO2) sequestration process from a gas feed stream containing carbon dioxide outputted from a power station, in accordance with an embodiment of the present invention. With additional reference to Fig. 2, the system is arranged to perform the process 100 of (i) in a first stage, mixing a slurry of chilled ground metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the ammonia/water/metal silicate solution to thereby absorb the carbon dioxide into a reactive solution; and (iii) passing the reactive solution through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate and produce a metal carbonate and by-product silica (stage three).\|[0040] In an embodiment, the slurry of ground metal silicate rock is chilled by circulating the slurry through a vessel in which ammonia evaporates. In an embodiment another stage is carried out prior to stage (ii), namely contacting flue gases in a vessel in a counter-current, staged manner so that residual ammonia in the flue gases is scrubbed from these gases to levels low enough to allow their final discharge in the atmosphere.\|[0041] In the illustrated embodiment the three stages are performed successively, with the first two stages occurring within a first apparatus 20 in the form of two separate reaction chambers, namely an absorption chamber 28 and a scrubbing chamber 30, and the last stage occurring within a reactor in the form of a pipeline 52 which may, for example, connect the mine site to the power plant. As will be described in detail in subsequent paragraphs of the specification, the reactor may alternatively take the form of an underground chamber (see Fig. 5) excavated at a sufficient depth to facilitate the conditions for the carbonation reactions to take place.\|[0042] The carbon dioxide sequestration process utilised in embodiments of the present invention is based on mineral carbonation. Mineral carbonation is a reaction between a metal-oxide bearing material and carbon dioxide. The metal-oxide bearing material may for example be alkaline-earth metals. Advantageously, the process 100 does not require the source of carbon dioxide to be particularly pure. In mineral carbonation, carbon dioxide reacts with the metal oxide bearing material to generate insoluble carbonates, that is to say:\| MO + CO2 → MCO3 + heat (1)\|which is an exothermic reaction, occurring more rapidly at elevated temperature, typically above 200°C. Certain chemicals may serve to increase the rate at which this reaction proceeds without being consumed themselves, i.e. they serve as catalysts. The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|[0043] The exact nature of the insoluble carbonates formed by the reaction depends on the metal-oxide bearing material. Suitable materials may be naturally occurring alkaline-earth metal-rich silicate rocks which contain mineral constituents such as serpentinite (Mg3Si2O5(OH)4), olivine (Mg2SiO4), orthopyroxene (MgSiO3), talc (Mg3Si4O10(OH)2) and wollastonite (CaSiO3). In practice, the element Iron (Fe) may substitute for some of the Magnesium (Mg) or Calcium (Ca). Other suitable materials include alkaline industry residues such as slag from steel production, the ash (both fly and bottom) from pulverised coal-fired boilers, the ash remaining from the combustion of paper recycling residues (de-inking ash), and cement. The amount of heat generated in the reaction will depend on the specific metal and on the mineral containing the metal oxide as can be seen below in the case of three natural silicates (heat values are given per unit mole of CO2 and at standard conditions (25°C and 0.1 MPa):\| Olivine\| Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 + 89 kJ mol-1 CO2 (2a)\| Serpentine\| Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol-1 CO2 (2b)\| Wollastonite\| CaSiO3 + CO2 → CaCO3 + SiO2 + 90 kJ mol-1 CO2 (2c)\|[0044] A preferred silicate rock (because of its greater abundance in continental land masses) comprises the mineral serpentine, Mg3Si2O5(OH)4, All of these minerals may be pre-treated to increase the surface area of rock that can come into direct contact with the carbon dioxide. In an embodiment, the pre-treatment involves crushing, grinding and/or milling of the mineral, as well as some mechanical classification and separation. Typically, these minerals would be wet-milled in ball mills or equivalent to form a finely ground metal silicate slurry (hereafter 'silicate slurry') 36 wherein 90% of the mineral matter was finer than 40 microns. However, the extent of the pre-treatment is dependent upon the source and type of mineral(s) being used in the process.\|[0045] With specific reference to Fig. 1, the carbon dioxide sequestration system 10 will now be described in detail. The system 10 receives a raw flue gas mixture feed stream 32 that has been generated and subsequently emitted by a power station (not shown). In the embodiment described herein, the raw flue gas mixture 32 is passed though a filter 34 to remove particulate matter. Suitable filters may include fabric filters, electrostatic precipitators and the like. Cleaning the raw flue gas mixture 32 serves to minimise both the maintenance costs in downstream gas-handling equipment and the concentrations of particulates in flue gases ultimately discharged to the atmosphere. It will be understood, however, that while desirable for process reasons, it is not essential that the raw flue gas mixture 32 be cleaned of particulates before it enters the scrubbing chamber 30.\|[0046] To maximise heat recovery in the system 10, the filtered flue gas mixture is then passed through a heat exchange apparatus in the form of a heat exchanger 34 so that the sensible heat of the filtered flue gas mixture (typically emitted at a temperature of around 135°C) is exchanged with the cooler gasses being expelled from the scrubbing chamber 30 of the first apparatus 20 and the filtered flue gas mixture is cooled to its water-vapour saturation temperature (i.e. to about 50°C). Suitable heat exchangers may include, for example, recuperative-type heat exchangers, such as the Ljungstrom rotary design as used for air pre-heating in power stations.\|[0047] As mentioned in preceding paragraphs, the carbon dioxide sequestration system 10 receives a source of silicate slurry 36. According to the embodiment described herein, the silicate slurry source is located near or at the mine site from which the silicate rocks are sourced. As previously described, the silicate mineral sourced from the mine site is finely ground (preferably by wet-milling in ball mills or equivalent to form the slurry) wherein 90% of the mineral matter is finer than 40 microns. The silicate slurry 36 is subsequently passed through a first pressure-exchange apparatus 38. To minimise power consumption, the pressure of the silicate slurry 36 may be increased by exchanging pressure with the final metal carbonate/silica product (hereafter `final product'), typically to a pressure of approximately 10 Bar. In addition, to minimize heat losses from the system 10 (and to ensure that the final product is cooled to a suitable temperature before it is emplaced in its final permanent repository), the silicate slurry 36 passes counter-currently through a second heat exchanger 40 to absorb the surplus sensible heat contained in the final product. At a second pressure-exchange apparatus 42, the pressure of the silicate slurry 36 is further increased, this time to a substantially higher level (typically 100 Bar). Again, this boost in pressure is achieved by exchanging pressure, but this time with the carbonate/silica slurry prior to it undergoing treatment in the ammonia gas recovery vessel 54 (as will be described in detail in subsequent paragraphs).\|[0048] A pipeline 44 connects the first apparatus 20 to the mine site and is used to transport the silicate slurry 36 used in the sequestration process 100. As will be described in more detail in subsequent paragraphs, an alternate path 52 in the pipeline 44, in this embodiment, also serves to act as a controlled reactor in which the metal carbonate reaction largely takes place. At or near to the power station site, the silicate slurry 36 is passed counter-currently through a third heat exchanger 46 and a third pressure-exchange apparatus 48, where the silicate slurry 36 is cooled and reduced in pressure by exchange with the reactive slurry discharged from the first apparatus 20, before being fed directly into the evaporator vessel 82, where ammonia which has passed through the expansion valve 29 and is now at a very low temperature, cools the silicate slurry to near freezing. To ensure that the silicate slurry 36 is not actually frozen, a portion of this slurry is circulated through the evaporator vessel. The chilled silicate slurry passes downwards through a vessel, the residual ammonia scrubber, in such a way that cleaned and cooled flue gases that have been stripped of most of their carbon dioxide content, pass upwards from below. There may be as many as six counter-current contacting stages, such that the cleaned, largely carbon dioxide-free flue gases may leave the system with less than one part per million of ammonia.\|[0049] The silicate slurry, now charged with any ammonia arriving in flue gases from below, enters the ammonia absorber 28, where it absorbs into solution all of the ammonia that is recovered in the ammonia recovery vessel 54 so as to produce a ammonia/water/metal silicate slurry.\|[0050] The ammonia is recycled from the ammonia gas recovery stage of the process (described in subsequent paragraphs), with additional quantities required only to make up for losses, which should be small. Recovered liquid ammonia (which may contain small amounts of water) is supplied to the absorption chamber 28 by way of a pipeline 60, under pressure. In a preferred embodiment, pressurised liquid ammonia passes through the pressure reduction valve 29, which reduces its pressure to near atmospheric, at which pressure it discharges into a vessel, the evaporator chamber 82, prior to entering the absorption chamber 28. A portion of the ammonia will flash to vapour upon entering the evaporator chamber 82. The ammonia, in vaporising, absorbs substantial quantities of latent heat which is withdrawn from the slurries circulating through banks of tubes in the evaporator chamber 82, thereby chilling them to near freezing. In the embodiment shown in Fig. 1, the heat absorbed as the ammonia vaporises is drawn from the silicate slurry used as the residual carbon dioxide scrubbing medium in the residual ammonia scrubbing chamber. This is to ensure that the scrubbing medium last in contact with the cooled, filtered flue gases is the most chilled.\|[0051] The vaporised ammonia flows from the evaporator chamber 82 directly into the ammonia absorption chamber 28, wherein it is rapidly absorbed into the deluging spray of circulating silicate slurry 36 after this has passed downwards through the several stages of the residual carbon dioxide scrubber, to produce the ammonia/water/metal slurry used as the circulating scrubbing medium for the carbon dioxide scrubbing chamber 30. When the ammonia is absorbed in the silicate slurry 36 a substantial quantity of heat is liberated: the heat of solution of ammonia gas in water. Much of this heat is removed as the slurry circulates through the heat exchanger 84. As illustrated, the heat exchanger 84 and cooling tower also serve to remove much of the excess low-grade heat generated from the absorption of the ammonia in the silicate slurry.\|[0052] The cooled filtered flue gas mixture passing through the heat exchanger 34 enters the scrubbing chamber 30 where the gas mixture passes upwards through deluging sprays of absorbent slurry, the absorbent slurry having been drawn from the ammonia absorption chamber 28 and discharged into the head space of the scrubbing chamber 30. When carbon dioxide is absorbed in the ammonia/water/metal silicate slurry, a further substantial quantity of heat is liberated, as carbon dioxide and ammonia form in solution a series of ammonium carbonate compounds. With sufficient ammonia supplied to the absorption chamber 28 to achieve 90 per cent capture of carbon dioxide, the tendency will be to form the bicarbonate NH4HCO3 in preference to the normal carbonate (NH4)2CO3 and the carbamate, NH2COONH4, which will also be present in smaller quantities, perhaps along with some urea, CO(NHZ)2. The system 10 is configured such that the coldest slurry will be the last to contact the stripped (of carbon dioxide) flue gas mixture, in such a way that ammonia slip (losses in final flue gases to the atmosphere) are essentially eliminated. In the embodiment shown in Fig. 1, the scrubbing chamber 30 is shown as being constructed separately to the absorption chamber 28. Suitable scrubbing chambers may be generally similar to the type used for flue gas desulphurisation.\|[0053] As previously described, the sensible heat is removed from the filtered flue gas mixture in the first heat exchanger 34, cooling it to around 50°C, before entering the scrubbing chamber 30. The clean flue gases exiting the scrubbing chamber 30 typically comprise around 95 per cent nitrogen and inerts by volume. The balance comprises some oxygen and around 1.5 per cent carbon dioxide, being the remnant quantity of this gas after some 90 per cent had been stripped out in the scrubbing chamber 30.\|[0054] The resultant product of this two-stage process is a reactive solution in the form of a metal silicate slurry in an aqueous phase that is itself primarily a solution of ammonium carbonates. A stream of the reactive ammoniated metal silicate slurry (hereafter 'reactive slurry') is drawn from the scrubbing chamber 30 and directed to the mine site via a return pathway 52 of the pipeline 44, which also advantageously acts as a controlled reactor. On route to the mine site, at or near to the power station, the reactive slurry is pressurised at the third pressure-exchange apparatus 48 to a high pressure of around 120 Bar (above the critical pressure of ammonia) and also heated to close to the boiling point of water at the pressure in question. Heating is accomplished firstly by transferring heat from the incoming silicate slurry arriving from the mine at the heat exchanger 46, and also by injection of steam 54. Without being bound by theory, the inventor anticipates that, subject to the process design assumptions of Example 1 (see table below), around 600 tonnes per hour of steam would be required to raise the temperature of the reactive slurry by around 100°C, to say 225°C, at which temperature the carbonation reactions are likely to reach acceptable rates. Heat liberated from the reaction between carbon dioxide and the metal silicate in the reactive slurry, which is highly exothermic, is capable on its own of raising the reactive slurry temperature by around 75°C (under the assumptions made in respect of Example 1), to yield a final temperature of some 300°C by the time the reactive slurry reaches the vicinity of the mine site, or site of other final emplacement. This temperature rise would be obtained despite some losses along the length of the return pipeline 52, notwithstanding attempts to minimise such losses by cladding this pipeline 52 throughout its length by suitable insulation (lagging).\|[0055] In the return pipeline 52 of the pipe reactor, most if not all of the carbon dioxide present in the reactive slurry can react with the silicate minerals and convert to insoluble carbonate during approximately the few first hours of transit. Each hour may correspond to a 10 kilometre length of this pipeline. In practice, however, the power station and the mine site may be much more than this distance apart, thereby allowing more than adequate time for reactions to proceed essentially to completion resulting in the metal carbonate product that contained most if not all of the carbon dioxide originally scrubbed from the power station flue gases. A high concentration of ammonia is maintained in the slurry throughout its passage from the power station to the mine/quarry or other emplacement site.\|[0056] When the final product in the return pipeline 52 reaches the vicinity of the mine site, as described above, it is passed through the second pressure-exchange apparatus 42 to lower the pressure of the stream from perhaps as high as 120 Bar to around 15-20 Bar, before entering the ammonia gas recovery vessel 54. With the temperatures indicated on Fig. 1, all of the ammonia and some of the water flash to vapours (the water would boil, the ammonia being driven out of solution) as the final product enters the ammonia gas recovery vessel 54, a consequence of a drop in temperature of more than 100°C. As shown in Fig 1, the hot pressurised final product transfers its sensible heat to the contents of the ammonia gas recovery vessel 54. This heat input assists to maximise the system's efficiency, as stripping the ammonia from the product as a gas absorbs considerable heat energy. To minimize the waste products generated by the system 10, and prior to entering the pipeline 44 for delivery to the continuous reactor 22, silicate slurry from the mine site is fed and re-circulated in the residual ammonia absorber 56 where residual vapours from the ammonia gas recovery vessel 54 are passed. A gas phase stream exiting from the top of the ammonia gas recovery vessel 54 contains essentially all of the free ammonia, which along with some water vapour condenses out in a condenser 58 to form a liquid phase that is mostly ammonia. In an embodiment, the condenser 58 is cooled by circulating water from dry (e.g. radiator-type) cooling towers, fin fan coolers, or, because no fans are required, a natural-draft cooling tower (not shown) such as used for cooling in the power station. This recovered liquid ammonia, representing the bulk of the ammonia injected into the circulating slurry in the absorption chamber 28, flows under pressure (aided by pumps, not shown) through an overland ammonia pipeline 60 to the power station site.\|[0057] The final product carbonate slurry (containing nearly all of the carbon dioxide in the original power station flue gases but now sequestered as carbonates), leaves the bottom of the ammonia gas recovery vessel 54. The final product slurry is free of ammonia, and in a form suitable for permanent emplacement in mine voids or other purpose-built repositories (not shown). In these emplacements the solids can settle and consolidate, releasing much of the aqueous phase as a clear supernatant. This supernatant may be collected and re-used in the process, for example, to prepare the silicate slurry 36 and returned to the power station site, via pipeline 44.\|[0058] It should be noted that not all of the ammonia added in the first apparatus 20 can be recovered and returned to the process via the overland ammonia pipeline 60. Some ammonia may end up as ammonium salts: sulphites and sulphates, and as ammonium nitrites and nitrates, from SOx and NOx respectively in the raw flue gases. If the raw flue gas source is a flue gas generated by a typical fossil fuel-fired power station, and assuming use of modern low-NOx burners, losses of ammonia via these reactions should will be minor. Their presence in the final carbonate product slurry may furthermore, assist with rehabilitation of the final emplacements of the carbonate minerals. Figure 1A illustrates an alternative embodiment including a residual ammonia scrubber positioned within the scrubbing chamber 30.\|[0059] It may be desirable to reduce the losses of ammonia that would occur in this way. In an embodiment, this is achieved by dosing, or otherwise adding to the reacted slurry immediately prior to its entry into the ammonia recovery vessel 58, an appropriate quantity of slaked lime or other suitable alkali. A source of such alkali may be power station fly ash or pulverised bottom ash. The presence of limestone or dolomite in the original coal may render them suitable for this duty; in passing through the boilers much of this limestone or dolomite will be converted to alkalis suitable for ammonia recovery: quicklime or dolime (dolomite-lime), respectively.\|[0060] Should it arise that the content of limestone or dolomite in the coal fuel is inadequate for the duty (as is likely to be the case with most power station fly ashes), it is possible to dose the appropriate quantity of pulverised limestone or dolomite to the power station boilers (not shown). This dosing may be conducted at a location in the hot combustion gas path where the gas temperatures are in the range 800-1,000°C, i.e. sufficient to convert these minerals to the reactive oxide forms (lime, or dolime respectively). For example, this may occur upstream of the boiler's economiser. When the ammonia-recovery vessel is close to the power station, as it would be in the case of the underground chamber reactor embodiment (Fig. 5), it may be appropriate to add all of the power station fly ash to the final product slurry to maximise the regeneration of ammonia for re-use in the process. In this manner, both fly ash and the final product slurry from the carbon sequestration process may be handled and co-disposed of as a single stream. An anticipated advantage stemming from the presence of fly ash having pozzolanic properties (a tendency to set in the presence of alkalis and moisture) in the final product, will assist with the rehabilitation process, by encouraging the final product/fly ash mix to "set".\|[0061] With reference to Fig. 3, there is shown an arrangement for the pressure-exchange apparatus described above. At the end of the reaction process, the pressure of the final carbonate-rich product must be reduced from approximately 120 Bar to atmospheric pressure. As described above, this is undertaken in two stages: from 120 Bar down to around 15 Bar, a pressure suitable for operation of the ammonia recovery stage, then from 15 Bar down to atmospheric pressure. Instead of merely reducing pressure by throttling valves, thereby losing the energy embodied in this pressure, the energy this pressure represents may be conserved by transferring it to the extent possible, in two stages, to the silicate slurry. In Fig. 3, slurry A comprises the products of the reactions that occur as the ammoniated, carbonated silicate slurry flow through the pipeline 44 from the power station to the mine site; while slurry B represents silicate slurry from the mine. A consequence of pressure exchange in these two stages is that slurry A's pressure would fall from around 120 Bar to near ambient pressure, while that of slurry B would rise: in the first stage (working from right to left) to around 10 Bar, then to perhaps 100 Bar in the second stage.\|[0062] Another pressure-exchange apparatus is also utilised at the power station site. Here, using the terminology of Fig. 3, slurry A represents the hot silicate slurry arriving via the pipeline from the mine; while slurry B comprises slurry exiting the scrubbing chamber 30 (i.e. silicate slurry now charged with ammonia and carbon dioxide, but at close to ambient pressures). A consequence of pressure exchange in this stage is that slurry A's pressure would fall from its arrival pressure (this may be 120 Bar, a pressure that would be maintained by booster pumping stations at strategic locations (not shown) along the pipeline 44 to overcome friction losses), to near ambient pressure. This pressure may be transferred (exchanged) to the extent possible to slurry B, thereby minimising the amount of pumping energy required to raise the pressure of this slurry to the levels required, here assumed to be 120 Bar. Since slurry A at this point will be at well below 120 Bar, pressure-exchange between slurries A and B alone may not be capable of raising the pressure of slurry B to 120 Bar. Also, the volume of slurry B may exceed that of slurry A. This is because of the much higher contents of carbon dioxide and ammonia, and of water condensed out of the power station flue gases. In an embodiment, additional pumping capacity may be installed to boost slurry B pressures to those required for the pipeline 44, and to pressurise those (relatively small) quantities of slurry B that cannot be pressurised by pressure-exchange with slurry A. For this function, conventional high-pressure diaphragm pumps, such as the Geho pump manufactured by Weir Netherlands b.v., may be implemented. This pumping, together with the pumping energy required to maintain pressures along the length of the pipelines, account for a substantial proportion of the total mechanical energy input to the total process. Other suitable pressure exchange/pump-turbine sets may comprise centrifugal pumps and radial-type hydraulic turbines. As the pressures are relatively high, the type of centrifugal pump may be a multi-stage barrel-type pump.\|[0063] With reference to Fig. 4 there is shown a configuration for the heat exchanger arrangements 40 & 46, according to an embodiment of the present invention. As previously discussed, high temperatures are required to initiate and accelerate the carbon sequestration reactions: the conversion of silicates to carbonates. These reactions, being exothermic, yield additional heat that can and should be applied to assist with creating the conditions needed for these reactions to proceed most efficiently. As shown, the heat exchanger arrangement is in the form of a simple shell-and-tube heat exchanger, consisting of two concentric pipes: the inner forms the "tube", the outer, the "shell". An advantage with this arrangement is that the heat exchanger can be made as long as is required to effect the desired transfer of heat: if necessary, many hundreds of metres long. For heat exchanger 40 (i.e. the heat exchanger on the mine site side), heat energy is transferred between the final carbonate/silica product (i.e. slurry A), which is hot, and the silicate slurry (slurry B), which is cool. For heat exchanger 46 (i.e. the heat exchanger on the power station side), slurry A would be hot silicate slurry from the mine, while slurry B would be slurry exiting the scrubbing chamber 30 (i.e. now charged with ammonia and carbon dioxide, but at close to ambient temperatures).\|[0064] Turning now to Fig. 5, there is shown an alternative system 200 for performing carbon dioxide sequestration which utilises (where geological conditions permit) an underground chamber as the reactor, as opposed to a pipeline reactor as illustrated in Fig. 1. In this embodiment, the reactor is in the form of a chamber 70 excavated from bedrock at a depth sufficient to allow the conditions for the core carbonation reactions to be generated entirely or partly by static head alone (e.g. 120 Bar for the carbonation reactions and 20 Bar for the recovery of ammonia gas from the reaction products). A chamber 70 excavated at a depth of approximately 1,000 meters and having a volume of 150,000 cubic meters, sufficient to allow for a 24 hours detention time for the contents, may be envisaged for holding the reactive slurry output from a system 200 fitted to an efficient 1,000MWe coal-fired power station. In practice a smaller chamber may suffice, should it arise that the reactions are essentially completed in less time.\|[0065] The silicate slurry 36 may be prepared either at the serpentine mine site and pumped overland to the power station site, or, the mineral could be railed, trucked or otherwise suitably transported to the power station site, and prepared there. Were the former course of action adopted, pipeline arrangements 44 would be considerably simpler than for the pipeline reactor embodiment described above with reference to Fig. 1. Specifically, the silicate slurry 36 would not be required to collect and transport heat and pressure energy from the mine site to the power station site, nor to host any residual ammonia. The pipeline 44 would simply be utilised for ore transport; whether it was transported as a lump product by rail or as slurry by pipeline would be determined mainly by economic considerations. It will be appreciated that in this embodiment, silicate slurry density could be substantially higher (e.g. 60 per cent solids), thereby reducing the volumes of silicate slurry required to be pumped, and allowing a lower pipeline velocity because of the reduced tendency for the solids in denser slurries to segregate and silt up the pipeline 44. Also, arrangements for conserving heat and pressure are much simpler than they would need to be for the pipeline reactor alternative.\|[0066] In Fig. 5, an injection pump 72 is utilised to drive the circulation of the reactive slurry from the scrubbing chamber 40, through a plurality of counter-current heat exchangers 74, 76, underground reactor 70 and ammonia gas recovery vessel 78 (flash/rectifying vessel) and back to the surface. It is envisaged that a formation of bubbles of ammonia gas may occur as the reacted slurry rises from the underground reactor 70 (a rise accompanied by a loss of static head, hence of pressure), thereby reducing the bulk density of the reacted slurry rising from the reactor. It follows that the required circulation could be achieved by entirely natural means: after the injection pump 72 has achieved the circulation necessary for the reaction to proceed, it may be taken off line. The design of injection pump 72 may be such that it could run backwards, that is to generate power, should the natural rate of circulation created by the buoyancy effect of ammonia bubbles forming in the reactor outlet pipe 80 be sufficiently strong.\|[0067] Heat exchangers 74, 76 are shown in schematic form at two locations on Fig. 5. In practice, the heat exchangers 74, 76 could be long, shell-and-tube designs, as shown in Fig. 4: they would span most of the vertical distance from the scrubbing chamber 40 down to the underground chamber 70. This is to say, whereas two separate pipelines are implied in Fig. 5, in practice, for most of their length they would be concentric: the annulus formed between the outer and concentric inner pipe would transport the hot reaction products, while the inner pipe would transport the products heading downward to the Reaction chamber. It will be understood by persons skilled in the art that this selection may be reversed.\|[0068] In contrast to the pipeline reactor configuration shown in Fig. 1, heating of the reactive slurry is accomplished by exchanging heat from the hot reaction products rising first from the ammonia gas recovery vessel 78, and as the raw slurry descended further, from hot slurry rising from the underground chamber 70. While some supplementary heat may be required, the heat generated by Equation 2(b) would be conserved, and available to heat raw reactive slurry.\|[0069] The design of the underground chamber 70 may be optimised to achieve some plug-flow characteristics. In an embodiment, the chamber 70 may have a high length-to-diameter ratio and be vertically aligned. In this manner, the incoming reactive slurry, being cooler hence slightly denser than the average contents of the reactive chamber 70, would tend to stratify at lower levels, displacing hotter slurry upwards. In an embodiment, the underground chamber 70 may be subdivided into two or more vertically stacked sub-chambers.\|[0070] There should be no requirement for separate agitation equipment in the reaction chamber to maintain the solids in suspension. As shown in Fig. 5, incoming reactive slurry enters the vessel close to its base, and it is envisaged that settling rates will be small relative to overall slurry up-flow rates. If, however, large residence times are required, implying in turn large reactor volumes, a form of agitation may be implemented.\|[0071] As will readily be appreciated, heat losses from the underground chamber 70 and pipelines may be much smaller than they would be even from a lagged above-ground pipeline and may be further reduced by insulation surrounding the reactor, pipelines and all other underground process vessels. Whereas an overland pipeline represents a plug-flow reactor, ideal conditions for a relatively slow series of reactions as are involved in carbon sequestration are also obtained in the embodiment illustrated in Fig. 5.\|[0072] Also in Fig. 5, an alternative ammonia absorption recovery process is utilised. In this embodiment, as the final product slurry rises from the underground chamber 70, the static head it experiences may decrease. A consequence of this is that the boiling point temperature will fall, eventually below that of the slurry rising in the products pipeline, leading to the flashing of some of the water to steam, and the stripping of ammonia from solution. As ammonia comes out of the solution as a gas it will absorb latent heat from the final product slurry, partially cooling it; the temperature would tend to track the boiling point of water at the prevailing pressure. The bubbles of ammonia will reduce the average density of slurry in the hot products pipeline to below that in the incoming reactants pipeline, leading to a pressure differential in the system that would serve to drive the circulation of the reactant and product slurries from the CO2 Absorber 30 and through the underground chamber 70, heat exchangers and other items of process plant. As shown on Fig. 5, the ammonia recovery vessel 78 and other necessary plant and equipment for recovering ammonia from the product slurries are installed at a level (perhaps 150 metres below ground level) that facilitate the use of static head to maintain a pressure in the vessel 78 of around 15 Bar, i.e. high enough so that ammonia was a liquid at near-ambient temperatures.\|[0073] As for the pipeline reactor case, the ammonia will be discharged as a gas from the top of the vessel 78, however due to the circumstances outlined above, this vessel 78 could be much simpler in design and, in an embodiment, need be little more than a gas-liquid separator. While some additional heat energy may be required to recover essentially all of the ammonia as a gas, typically as steam, with the arrangements proposed the heat-energy burden of carbon sequestration could be greatly reduced.\|Examples\|[0074] Again with specific reference to Fig. 2, a non-limiting example process flow for carbon sequestration for the first system configuration 10 described herein (i.e. the system depicted in Fig. 1) will now be given, wherein for convenience, like parts to those shown in the foregoing embodiment have been numbered with like numerals.\|Example 1\|[0075] Table 1: Indicative mass and heat balance figures from 1.000 MWe of black coal-fired electricity generation plant.MaterialPer yearPer hourTotal CO2 generated:6.4 106 t800 tSilicate rock to absorb 90% of this CO2:145m 106 t1,800 tWater required to make 30% by wt slurry:33.6 106 t4,200Ammonia to conv. 90% of CO2 to (NH4)2CO3:4.45 106 t560 tHeat liberated (3.6 GJ/t CO2):2,800 GJTotal slurry with (NH4)2CO3:58 106 t7,2501Slurry density:1.3 t/m31.3 t/m3Slurry pipe dia. (both with 2 m/s velocity:1.0 m1.0 metresAmmonia pipe diameter, 2 m/s velocity0.4 m0.4 metresConc. of ammonia in Absorber aq. phase:12% (by wt)12%Ammonia lost due to SOx16,000 t2.0 tAmmonia lost due to NOx3,000 t0.37 tOther losses of ammonia:11,000 t1.38 tAmmonia make-up % of flow to Absorber:0.67%0.67%\|[0076] Table 1 provides a detailed mass and heat balance for a carbon dioxide sequestration process, assuming:\| 90 per cent carbon dioxide capture and sequestration from 1,000 MWe of black coal-fired electricity generation plant, which when operating in base-load mode might expect to generate annually 8,000 GWh of electricity;\| where on a dry ash-free basis, the coal is 81.3% by weight carbon and 0.65% sulphur (as S) and the flue gases contain 400 ppm NOx.\|[0077] The heat of formation of ammonium carbonate in solution from ammonia, water and carbon dioxide is around 2.0 GJ/tonne carbon dioxide equivalent, sufficient to heat the slurry by 75°C. Offsetting this is the heat absorbed when each tonne of ammonia is vaporised in the absorption zone, around 1.0 GJ/tonne ammonia. This is equivalent to around 1.8 GJ per tonne of carbon dioxide absorbed, sufficient to cool the slurry feed by around 60°C. It follows that there would be an overall temperature rise between the time the slurry feed enters the absorption zone and the time it enters the return pipeline 52, of around 15°C. In practice, it may be necessary to design the process so that the last slurry feed that the final largely carbon dioxide free flue gases is the coldest: less than 5°C.\|[0078] As well, the heat released when ammonium carbonate in solution reacts with the silicate rocks, roughly 1.45 GJ/tonne carbon dioxide absorbed, is sufficient to raise the temperature of the slurry feed by around 55°C. This occurs in the return pipeline 52.\|[0079] At the mine, the condensation of around 300 tonnes per hour of ammonia would release some 160 MWt of heat energy, which can be rejected to the environment via a cooling tower.\|[0080] An advantage of the carbon dioxide sequestration process 100 and systems 10, 20 according to embodiments of the present invention is that by selecting ammonia as a catalyst/promoter, a single integrated process can be provided for both capture and sequestration of carbon dioxide. In an embodiment, sequestration of the carbon dioxide takes place in a reactor, in the form of a return pathway 52 of a pipeline 44, which advantageously connects the power station (i.e. the source of carbon dioxide) to the source/destination of the absorbent material being used in the process. In an alternative embodiment, where geological conditions permit, the reactor may take the form of an underground chamber which advantageously facilitates the reaction without requiring pressure-exchange and head-recovery equipment required for the pipeline embodiment. Another advantage of the carbon dioxide sequestration process and systems is that the reaction kinetics may be improved by using ammonia. Therefore, by using ammonia and exploiting the heat generated by the exothermic reaction, the energy consumption of the process 100 can be kept to a minimum. As the reaction products are thermodynamically stable, carbon dioxide can be stored in a permanent stable solid form. Following from this, further advantages include lower operating and capital costs.\|[0081] Persons skilled in the art will appreciate that further advantages may arise from carrying out certain steps of the aforementioned embodiments in isolation. For example, the catalytic effect of a solution of ammonia with an ammonium salt (that may be ammonium carbonate formed by exposing an ammonia-rich solution to a gas stream containing carbon dioxide) in the carbon dioxide sequestration process can also be utilised for extracting metals (e.g. magnesium, iron, nickel, copper and other metals present in the silicate rock) from metal silicates, such as magnesium-rich metal silicates. In such an embodiment a solution comprising ammonia and ammonium may be mixed with a metal silicate (typically in slurry form) to allow the dissolution of magnesium ions by ammonia to recover the metal, in this embodiment a metal compound in the form of magnesium carbonate. The mixing may occur in an ammonia absorption chamber such as that previously described in connection with the preceding embodiments. Preferably the ammonia solution comprises concentrated ammonia in the presence of ammonia salts in solution, such as ammonium carbonate, to prevent the precipitation of magnesium hydroxide, hence allowing the dissolution of magnesium ions by ammonia to continue. A further advantage arising from this process is that after extraction of magnesium carbonate, other minerals (metals) present within the silicate rock are also amenable to recovery. The silicate rock may comprise mafic or ultra-mafic rocks (i.e. rocks with a high magnesium content).\|[0082] The catalytic effect of the ammonia follows from its tendency to form complexes (ammines) with certain metal ions including magnesium (Mg2+), divalent iron (Fe2+), copper (Cu2+) and nickel (Ni2+). The presence of ammonium salts notably the carbonate formed from the reaction between ammonia and carbon dioxide prevents precipitation of the otherwise insoluble magnesium hydroxide. Magnesium carbonate is however insoluble in such an environment, so a precipitate of this compound will form from the reaction between magnesium hydroxide and ammonium carbonate, to yield ammonium hydroxide and free ammonia in solution, the latter continuing to extract additional magnesium and other metals from the silicate rock through formation of ammine complexes until all such susceptible metals have been extracted.\|[0083] Subsequently, the ammonia is recovered from the solution by in the ammonia recovery vessel, a consequence being a progressive reduction in the concentration of free ammonia in the reactive slurry. This leads to destruction of the metal ammine complexes, but in a progressive manner, depending on the stability of the complexes, which stability in turn differs between metals. Those of magnesium are relatively weak (the reason most of the magnesium will have precipitated out as magnesium carbonate), so the first salt to be precipitated is further magnesium carbonate. As the concentration of ammonia in solution continues to fall, other metals can precipitate in sequence, allowing the opportunity of obtaining precipitates of each single metal in relatively pure form.\|[0084] Finally, it is to be appreciated that various alterations or additions may be made to the parts previously described without-departing from the spirit or ambit of the present invention as defined by the following claims. The process is not limited to having a single two-stage continuous reactor, or a single tube-like reactor, as the process may be arranged to utilise alternatively configured items of equipment as necessary to accommodate process variables, arising from different source materials, capital and operating costs. For example, in the exemplary embodiment previously described the plant design is based on the emission of 800 tonnes CO2/GWh generated from a state-of-the-art black coal-fired electricity generation plant. By comparison, the Bayswater Power Station and the Liddell Power Station, both in the Hunter Valley of New South Wales, Australia, able to generate 2,640 MWe and 2,040 MWe respectively, being older hence less efficient can be expected to emit between 850 and 900 tonnes CO2/GWh.\|[0085] Thus the concentration and rate of carbon dioxide emissions in the flue gas emitted by the power plant may vary such that the plant equipment design may be reconfigured to accommodate these variables. For example, alternative equipment can be configured for the various heat and pressure exchange stations. The carbon dioxide absorption zone and the scrubbing zone may be arranged in series in two separate vessels (rather than the nested configuration shown in Fig. 1). The conversion of carbon dioxide to insoluble carbonates may be limited to a lower value, such as 70% whilst still obtaining a good overall conversion from the reactor(s). As well, the corresponding solids concentration in the slurry feed may be higher or lower than 30% solids by weight. It is possible that the metal silicate solution may comprise a blend of metal silicates, e.g. mixture of serpentines and olivines, even pyroxenes. The reaction kinetics may require heat to be removed from the reactive solution (rather than heat addition as described above). These factors will impact and alter the system pressures. There might be two or more pipelines for transporting the metal silicate solution and the reactive solution; because there are more pipelines additional heat exchangers and pressure-exchange apparatus may be used. The power station flue gas may include additional pre-processing steps including flue gas desulphurisation (FGD) and selective catalytic reduction (SCR) to reduce concentrations of SOx and NOx respectively hence losses of ammonia from the system. Furthermore, the availability of services, such as steam and cooling water may require different equipment arrangements.\|[0086] Any reference to prior art contained herein is not to be taken as an admission that the information is common general knowledge, unless otherwise indicated.\|[0087] In the claims which follow and in the preceding description of the invention, except where the context requires otherwise due to express language or necessary implication, the word "comprise" or variations such as "comprises" or "comprising" is used in an inclusive sense, i.e. to specify the presence of the stated features but not to preclude the presence or addition of further features in various embodiments of the invention.	Family Number\|(6597398)\|6597398\|Object of Invention\|(AU2008217572 B2)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|In accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|(AU2009250983 A1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|In accordance with a third aspect of the present invention, in a pipeline, there is provided a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|(CA2678800 C)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(CA2678800 A1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(CN101641145B B)\|A first aspect of the invention provides a method of carbon dioxide sequestration , the method comprising the steps of : \|The present invention relates generally to systems , apparatus and methods for carbon dioxide sequestration and more particularly , but not exclusively , to systems and methods for the capture and sequestration of carbon dioxide from power plant flue gases . \|The present invention relates to a method for carbon dioxide sequestration comprising the following steps . \|(CN101641145 A)\|A first aspect of the invention provides a method of carbon dioxide sequestration , the method comprising the steps of : \|The present invention relates generally to systems , apparatus and methods for carbon dioxide sequestration and more particularly , but not exclusively , to systems and methods for the capture and sequestration of carbon dioxide from power plant flue gases . \|The present invention relates to a method for carbon dioxide sequestration comprising the following steps . \|(EP2134449 B1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with (...) \|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(JP5345954 B2)\|The present invention relates generally to systems, apparatuses, and methods for carbon dioxide isolation, and more particularly to (but not limited to) systems and methods for capturing and isolating carbon dioxide from power plant flue gases.\|(JP2010519027 A)\|The present invention relates generally to systems, apparatuses, and methods for carbon dioxide isolation, and more particularly to (but not limited to) systems and methods for capturing and isolating carbon dioxide from power plant flue gases.\|(KR101527365 B1)\|A first aspect of the present invention is a process for producing ammonia/water/metal silicate slurry, the process comprising the steps of: (i) mixing ammonia with a slurry of metal silicate rock to produce an ammonia/water/metal silicate slurry; (ii) scrubbing a carbon dioxide-containing gas stream with the solution obtained from the first step (i), A second step of absorbing carbon dioxide into the reactive slurry; and (iii) a third (...) \|The present invention relates to systems, apparatuses and methods for carbon dioxide isolation, and more particularly, but not exclusively, to apparatuses and methods for capturing and isolating carbon dioxide from power plant flue gases.\|(KR20090125109 A)\|A first aspect of the present invention is a process for producing ammonia/water/metal silicate slurry, the process comprising the steps of: (i) mixing ammonia with a slurry of metal silicate rock to produce an ammonia/water/metal silicate slurry; (ii) scrubbing a carbon dioxide-containing gas stream with the solution obtained from the first step (i), A second step of absorbing carbon dioxide into the reactive slurry; and (iii) a third (...) \|The present invention relates to systems, apparatuses and methods for carbon dioxide isolation, and more particularly, but not exclusively, to apparatuses and methods for capturing and isolating carbon dioxide from power plant flue gases.\|(US8496897 B2)\| (...) This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|(US20100021362 A1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(WO2008101293 A1)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|Technical Field This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(IN-293376 B)\|In a first aspect the present invention provides a carbon dioxide sequestration process including the steps of:\|This invention relates generally to a system, apparatus and method for carbon dioxide sequestration and more particularly, but not exclusively, to a system and method for the capture and sequestration of carbon dioxide from power station flue gases.\|(IN2009DN06026 A)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. (...) \|Abstract\|(AU2008217572 B2)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From US8496897 B2)\|(AU2009250983 A1)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From US8496897 B2)\|(CA2678800 C)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|(CN101641145B B)\|A carbon dioxide sequestration process includes the following steps . In a first stage , a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia / water / metal silicate slurry . In a second stage , the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry . In a third stage , the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate . \|(EP2134449 B1)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|(KR101527365 B1)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.COPYRIGHT KIPO & WIPO 2010\|(US8496897 B2)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|(WO2008101293 A1)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|(IN-293376 B)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.\|Title\|(AU2008217572 B2)\|System, apparatus and method for carbon dioxide sequestration\|(AU2008217572 A1)\|System, apparatus and method for carbon dioxide sequestration\|(AU2009250983 A1)\|System, apparatus and method for carbon dioxide sequestration\|(CA2678800 C)\|System, apparatus and method for carbon dioxide sequestration\|(CA2678800 A1)\|System, apparatus and method for carbon dioxide sequestration\|(CN101641145B B)\|System , apparatus and method for carbon dioxide sequestration \|(CN101641145 A)\|System , apparatus and method for carbon dioxide sequestration \|(EP2134449 B1)\|System, apparatus and method for carbon dioxide sequestration\|(EP2134449 A4)\|System, apparatus and method for carbon dioxide sequestration\|(EP2134449 A1)\|System, apparatus and method for carbon dioxide sequestration\|(KR101527365 B1)\|System, apparatus and method for carbon dioxide sequestration\|(KR20090125109 A)\|System, apparatus and method for carbon dioxide sequestration\|(US8496897 B2)\|System, apparatus and method for carbon dioxide sequestration\|(US20100021362 A1)\|System, apparatus and method for carbon dioxide sequestration\|(WO2008101293 A1)\|System, apparatus and method for carbon dioxide sequestration\|(IN-293376 B)\|System, apparatus and method for carbon dioxide sequestration\|(IN2009DN06026 A)\|System, apparatus and method for carbon dioxide sequestration\|Advantages / Prev. Drawbacks\|(AU2008217572 B2)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(AU2009250983 A1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(CA2678800 C)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(CA2678800 A1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(CN101641145B B)\|The inventors have found that the use of ammonia as catalyst has particular advantages : it can be used both for separating carbon dioxide from a gas mixture ( called carbon capture ) and for its permanent isolation in a single integrated process . \|(CN101641145 A)\|The inventors have found that the use of ammonia as catalyst has particular advantages : it can be used both for separating carbon dioxide from a gas mixture ( called carbon capture ) and for its permanent isolation in a single integrated process . \|(EP2134449 B1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(US8496897 B2)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(US20100021362 A1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(WO2008101293 A1)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|(IN-293376 B)\|The present inventor has discovered that using ammonia as a catalyst has the particular advantage of being able to use a single integrated process for both the isolation of carbon dioxide from a mixture of gases, known as carbon capture, and for its permanent sequestration.\|Independent Claims\|(AU2008217572 B2)\|1. A carbon dioxide sequestration process including the steps of:(i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (...) \|27. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|(AU2009250983 A1)\|1. A carbon dioxide sequestration process including the steps of:(i) in a fast stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (...) \|27. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|33. In an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, the steps of: (...) \|(CA2678800 C)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the ammonia/water/metal silicate slurry from (i) to thereby absorb the carbon dioxide into a (...) \|(CA2678800 A1)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the ammonia/water/metal silicate slurry from (i) to thereby absorb the carbon dioxide into a (...) \|(CN101641145B B)\|1. A method of carbon dioxide sequestration , the method comprising the steps of : ( i ) in a first stage , mixing a slurry of metal silicate rock with ammonia to produce an ammonia / water / metal silicate slurry ; ( . . . ) \|(CN101641145 A)\|1. A method of carbon dioxide sequestration , the method comprising the steps of : ( i ) in a first stage , mixing a slurry of metal silicate rock with ammonia to produce an ammonia / water / metal silicate slurry ; ( . . . ) \|27. In a pipeline , providing a first flow path with a metal silicate slurry for use by a first apparatus in a carbon sequestration process ; and a second flow path with the reactive slurry from the first apparatus and comprising carbon dioxide absorbed in the ammonia / water / metal silicate slurry , wherein the second flow path is controlled to promote the reaction of carbon ( . . . ) \|33. In an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia to produce an ammonia / water / metal silicate slurry for use in a carbon dioxide sequestration process , the following steps are provided : ( . . . ) \|(EP2134449 B1)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) (...) \|(KR101527365 B1)\|1. A method of carbon dioxide sequestration comprising: (i) A method for producing a metal silicate, comprising: a first step of mixing a slurry of metal silicate rock with ammonia to produce a slurry composed of ammonia/water/metal silicate; (ii) A second step of scrubbing the carbon dioxide (...) controlled in order to promote the reaction between carbon dioxide and the metal silicate and to produce metal carbonate, Carbon dioxide sequestration method.\|(KR20090125109 A)\|1. A method of carbon dioxide sequestration comprising: (i) A first step of mixing ammonia with a slurry of metal silicate rock to produce an ammonia/water/metal silicate slurry; (ii) A second step of scrubbing the carbon dioxide containing gas flow (...) controlled reactor in order to promote the reaction between carbon dioxide and the metal silicate and produce metal carbonate, Carbon dioxide sequestration method.\|27. A pipeline, comprising: A first flow path carrying metal silicate for use by a first device in a carbon sequestration process; and A second flow path carrying the reactive slurry from the first device and comprising carbon dioxide absorbed in the ammonia/water/metal silicate slurry, Wherein the second flow path is controlled to cause carbon dioxide to react (...) \|33. An ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia to produce ammonia/water/metal silicate for use in a carbon dioxide sequestration process, (i) Bringing ammonia into pressurized liquid form to expand in an evaporator stage to provide a cooling effect in said evaporator stage prior to passing it through an absorption process; and (ii) Passing the ammonia/water/metal silicate (...) \|(US8496897 B2)\|1. A carbon dioxide sequestration process including the steps of: (i) providing a slurry comprising metal silicate rock; (ii) in a first stage, mixing the slurry of metal silicate rock with ammonia so as to produce an ammonia/water/metal silicate slurry; (iii) in a second stage, scrubbing a gas stream containing carbon dioxide with the slurry from (ii) to thereby absorb the carbon dioxide into the slurry so as to form a reactive (...) \|18. An ammonia absorption process in a carbon dioxide sequestration process, the ammonia absorption process comprising the steps of: (i) producing a slurry of metal silicate rock mixed with ammonia so as to produce an ammonia/water/metal silicate slurry; (ii) provide pressurized ammonia in liquid form; (iii) expanding the pressurized ammonia in liquid form in an evaporator stage so as to provide a cooling effect in (...) \|(US20100021362 A1)\| (...) A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) (...) \| (...) In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \| (...) In an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, the steps of: (i) prior to passing the ammonia to the absorption process, allowing the ammonia in pressurised liquid form to expand in an evaporator stage so as to provide a cooling effect in that stage; and (ii) passing the ammonia/water/metal (...) \|(WO2008101293 A1)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) (...) \|27. In a pipeline, the provision of a first flow path that carries a metal silicate slurry for use by a first apparatus in a carbon sequestration process; and a second flow path that carries a reactive slurry from the first apparatus and which comprises carbon dioxide absorbed in an ammonia/water/metal silicate slurry, wherein the second flow path is controlled so as to encourage the (...) \|33. In an ammonia absorption process in which a slurry of metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry for use in a carbon dioxide sequestration process, the steps of: (i) prior to passing the ammonia to the absorption process, allowing the ammonia in pressurised liquid form to expand in an evaporator stage so as to provide a cooling effect in that stage; and (ii) passing the ammonia/water/metal (...) \|(IN-293376 B)\|1. A carbon dioxide sequestration process including the steps of: (i) in a first stage, mixing a slurry of a metal silicate rock with ammonia so as to produce a ammonia/water/metal silicate slurry; (ii) in a second stage, scrubbing a gas stream containing carbon dioxide with the solution from (i) to thereby absorb the carbon dioxide into a reactive slurry; and (iii) (...) \|	Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-2251/2062\|B01D-2251/402\|B01D-2257/504\|C01B-032/50\|C01B-032/60\|C01B-033/20\|C01F-005/24\|Y02A-050/20\|Y02C-020/40\|Y02P-020/151		B01D-053/62\|B01D-2251/2062\|B01D-2251/402\|B01D-2257/504\|C01B-032/50\|C01B-032/60\|C01B-033/20\|C01F-005/24\|Y02A-050/20\|Y02C-020/40\|Y02P-020/151	B01D-053/14\|B01D-053/62\|B01D-053/80\|C01B-031/20\|C01B-032/50\|C01B-032/60\|C01B-033/20\|C01B-033/24\|C01F-005/24	B01D-053/14\|B01D-053/62\|B01D-053/80\|B01J-008/20\|C01B-031/20\|C01B-031/24\|C01B-032/50\|C01B-032/60\|C01B-033/20\|C01B-033/24\|C01F-005/24	PCLO=423230000\|PCLX=423234000\|PCLX=423352000\|PCLX=423331000	PCLO=423230000 PCLX=423234000 PCLX=423331000 PCLX=423352000\|PCLO=423230000 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K. O, CONNOR, ET AL: "Carbon dioxide sequestration by direct mineral carbonation : process mineralogy of feed and products", 《 2001SME ANNUAL MEETING&EXHIBIT》 (Cat. X)\|S.J.Gerdemann et al..THE GRAVITY-PRESSURIZED REACTOR AS A MEANS TO EFFICIENTLY CARRY OUT METALLURGICALLY IMPORTANT REACTIONS.《chemical engineering science》.1992,第47卷(第13/14期),3753-3760.\|特開2005−097072(JP,A)\|国際公開第2004/094043(WO,A1)	WO200608242; WO2005108297; WO200498740; WO200494043; WO200608242; WO200494043; WO2005108297; WO200498740; WO200622885\|\|\|\|JP2005097072; JP5345954\|WO200498740; WO200608242; WO200494043; CN1106311; WO2004098740; WO2005108297; WO2006008242; WO2004094043\|JP2005097072; WO200494043\|US4226277; US2829060; US4308241; WO200608242; CN1106311; JP2005097072; WO200494043; WO200498740; WO2005108297; WO200608242\|WO200608242; WO2005108297; WO200498740; WO200494043; XP002619884; WO200608242; WO200494043; WO2005108297; WO200498740; WO200622885\|WO2005108297; WO200608242; WO200498740	(EP2134449)\|Search Report references [Examiner]\|-See also references of WO 2008101293A1\|-GERDEMANN S J ET AL: "Gravity-pressurized reactor as a means to efficiently carry out metallurgically important reactions", CHEMICAL ENGINEERING SCIENCE 1992 SEP-OCT,, vol. 47, no. 13-14, 1 September 1992 (1992-09-01), pages 3753 - 3760, XP002619884\|\|(US8496897)\|Pre-Search references [Examiner]\|-Sugiyama, "Phase Diagram." 8/24/2002. Downloaded 12/17/09 from http://www.gfd-dennou.org/library/oboro/gallery/output/phase/index.html.en .\|-Fauth et al., "Carbon dioxide storage as mineral carbonates." ACS Div. of Fuel Chem. Preprints, Vol. 45, Issue 4, 2000 (no month), pp. 708-712.\|-Ophardt, Charles E., "Virtual Chembook." Elmhurst College (2003). Viewed 8/12/12 at http://www.elmhurst.edu/~chm/vchembook/174temppres.html .\|-Simtronics Corp., "SPM-3100 Amine Treating Unit." Published 2006. Viewed 8/12/12 at http://www.simtronics.com/catalog/spm/spm3100.htm .\|-English translation of second office action issued Apr. 5, 2012 by State Intellectual Property Office of P.R. China for corresponding Chinese application 200880006610.5.\|-Sugiyama, "Phase Diagram." Aug. 24, 2002. Downloaded Dec. 17, 2009 from http://www.gfd-dennou.org/library/oboro/gallery/output/phase/index.html.en.\|-Fauth et al., "Carbon dioxide storage as mineral carbonates." ACS Div. of Fuel Chem. Preprints, vol. 45, Issue 4, 2000 (no month), pp. 708-712.\|-Ophardt, Charles E., "Virtual Chembook." Elmhurst College (2003). Viewed Aug. 12, 2012 at http://www.elmhurst.edu/~chm/vchembook/174temppres.html.\|-Simtronics Corp., "SPM-3100 Amine Treating Unit." Published 2006. Viewed Aug. 12, 2012 at http://www.simtronics.com/catalog/spm/spm3100.htm.\|\|(WO2008/101293)\|Applicant references\|-See also references of EP 2134449A4\|\|\|\|\|\|\|\|	GRANTED	(EP2134449)\|LAPSED\|(US8496897)\|LAPSED\|(WO2008/101293)\|LAPSED\|(JP5345954)\|LAPSED\|(CN101641145)\|LAPSED\|(IN293376)\|GRANTED\|(CA2678800)\|LAPSED\|(KR10-1527365)\|LAPSED\|(AU2008217572)\|EXPIRED\|(AU2009250983)\|LAPSED	ALIVE	(EP2134449)\|DEAD\|(US8496897)\|DEAD\|(WO2008/101293)\|DEAD\|(JP5345954)\|DEAD\|(CN101641145)\|DEAD\|(IN293376)\|ALIVE\|(CA2678800)\|DEAD\|(KR10-1527365)\|DEAD\|(AU2008217572)\|DEAD\|(AU2009250983)\|DEAD	(EP2134449)\|LEGAL DETAILS FOR EP2134449\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP08706115\|Application date=2008-02-20\|Standardized application number=2008EP-0706115\|Event publication date=2009-11-20\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2009-12-23\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2134449\|Publication stage code=A1\|Publication date=2009-12-23\|Standardized publication number=EP2134449\|Event publication date=2009-12-23\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2009-09-17\|Event publication date=2009-12-23\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR\|Event publication date=2010-05-26\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2011-03-30\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP2134449\|Publication stage code=A4\|Publication date=2011-03-30\|Standardized publication number=EP2134449\|Event publication date=2011-03-30\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2011-02-25\|Event publication date=2011-11-09\|Event code=EP/17Q\|Event indicator=Pos\|Event group=Examination events\|First examination report\|Erster pruefungsbescheid\|Effective date of the event=2011-10-11\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-18\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2012-04-25\|Event code=EP/GRAP\|Event indicator=Pos\|Event group=Examination events\|DESPATCH OF COMMUNICATION OF INTENTION TO GRANT A PATENT\|New entry: 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EFFECT AS A NATIONAL PATENT IN CH/LI\|Wirkung des europäischen patents als nationales patent in ch/li tritt ein\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2013-09-30\|Event code=EP/REG\|Event code=CH/PL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent ceased\|Loeschung/radiation/radiazion\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2013-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=CH\|MEMBER STATE LEGAL DETAILS FOR CY\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CY\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event 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date=2018-09-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE Corresponding appl: DE602008019269\|Event publication date=2012-03-12\|Event code=EP/REG\|Event code=DE/R079\|Event group=Corrections\|Reference to a national code\|Amendment of ipc main class\|Aenderung der IPC hauptklasse\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2012-03-12\|Event code=EP/REG\|Event code=DE/R079\|Event group=Corrections\|Reference to a national code\|Amendment of ipc main class\|Aenderung der IPC hauptklasse\|Previous main class: B01D0053620000\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2012-12-06\|Event code=EP/REG\|Event code=DE/R096\|Event indicator=Pos\|Event group=Examination events\|Reference to a national code\|DPMA publication of mentioned EP patent grant\|Veroeffentlichung eines hinweises auf die ep-patenterteilung durch das dpma\|Effective date of the event=2012-12-06\|Corresponding cc:\|Designated 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notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=DK\|MEMBER STATE LEGAL DETAILS FOR EE\|Actual or expected expiration date=2013-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EE\|Event publication date=2013-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=EE\|MEMBER STATE LEGAL DETAILS FOR ES\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=ES\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=ES\|MEMBER STATE LEGAL DETAILS FOR FI\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=FI\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member 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In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2017-02-17\|Year of payment of annual fees=10\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2018-11-30\|Event code=EP/REG\|Event code=FR/ST\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Notification of lapse\|Constatation de decheances\|Effective date of the event=2018-10-31\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2019-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=FR\|MEMBER STATE LEGAL DETAILS FOR GB\|Actual or expected expiration date=2018-02-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2012-10-10\|Event code=EP/REG\|Event code=GB/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patent granted\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2017-02-16\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2017-02-16\|Year of payment of annual fees=10\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2018-02-20\|Event code=EP/GBPC\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|GB: European patent ceased through non-payment of renewal fee\|Effective date of the 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DETAILS FOR HR\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=HR\|MEMBER STATE LEGAL DETAILS FOR HU\|Actual or expected expiration date=2015-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HU\|Event publication date=2015-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO\|Corresponding cc:\|Designated or member state=HU\|MEMBER STATE LEGAL DETAILS FOR IE\|Actual or expected expiration date=2013-12-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2012-11-07\|Event code=EP/REG\|Event code=IE/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patents granted designating Ireland\|European patent granted\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2013-12-04\|Event code=EP/REG\|Event code=IE/MM4A\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent lapsed\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2014-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=IE\|MEMBER STATE LEGAL DETAILS FOR IS\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IS\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IS\|MEMBER STATE LEGAL DETAILS FOR IT\|Actual or expected expiration date=2013-08-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2013-08-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IT\|MEMBER STATE LEGAL DETAILS FOR LI\|Actual or expected expiration date=2013-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LI\|Event publication date=2013-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LI\|MEMBER STATE LEGAL DETAILS FOR LT\|Actual or expected expiration date=2013-03-25\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2013-03-25\|Event code=EP/REG\|Event code=LT/MG4D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Invalidated european patent\|Europos patentai, laikomi ab initio negaliojanciais\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LT\|MEMBER STATE LEGAL DETAILS FOR LU\|Actual or expected expiration date=2015-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LU\|Event publication date=2015-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LU\|MEMBER STATE LEGAL DETAILS FOR LV\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LV\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LV\|MEMBER STATE LEGAL DETAILS FOR MC\|Actual or expected expiration date=2013-09-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MC\|Event publication date=2013-09-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=MC\|MEMBER STATE LEGAL DETAILS FOR MT\|Actual or expected expiration date=2014-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MT\|Event publication date=2014-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MT\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=2012-10-10\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2013-03-13\|Event code=EP/REG\|Event code=NL/VDEP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Invalid in the netherlands as no translation has been filed\|Verval wegens niet indienen vertaling\|Effective date of the event=2012-10-10\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NL\|MEMBER STATE LEGAL DETAILS FOR NO\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NO\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NO\|MEMBER STATE LEGAL DETAILS FOR PL\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PL\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PL\|MEMBER STATE LEGAL DETAILS FOR PT\|Actual or expected expiration date=2013-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PT\|Event publication date=2013-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PT\|MEMBER STATE LEGAL DETAILS FOR RO\|Actual or expected expiration date=2013-08-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RO\|Event publication date=2013-08-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RO\|MEMBER STATE LEGAL DETAILS FOR SE\|Actual or expected expiration date=2013-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2013-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SE\|MEMBER STATE LEGAL DETAILS FOR SI\|Actual or expected expiration date=2013-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SI\|Event publication date=2013-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SI\|MEMBER STATE LEGAL DETAILS FOR SK\|Actual or expected expiration date=2013-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SK\|Event publication date=2013-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SK\|MEMBER STATE LEGAL DETAILS FOR TR\|Actual or expected expiration date=2015-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=TR\|Event publication date=2015-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=TR\|(US8496897)\|LEGAL DETAILS FOR US8496897\|Actual or expected expiration date=2021-09-06\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US12527608\|Application date=2008-02-20\|Standardized application number=2008US-12527608\|Event publication date=2008-02-20\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:BERNS, DANIEL J\|Event publication date=2008-02-20\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2008-02-20\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 930125-2009\|Event publication date=2008-02-20\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 20999\|Event publication date=2008-02-20\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2008-02-20\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2009-08-18\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2009-08-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2009-10-16\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2009-10-16\|Event code=US/M903\|Event indicator=Pos\|Event group=Examination events OAO\|Notice of DO/EO Acceptance Mailed\|Event publication date=2009-12-14\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2010-01-28\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20100021362\|Publication stage code=A1\|Publication date=2010-01-28\|Standardized publication number=US20100021362\|Event publication date=2010-01-28\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2010-10-06\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-07-06\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-07-14\|Event code=US/RESTREQ\|Event group=Examination events Corrections OAO\|Restriction/Election Requirement\|Event publication date=2011-08-15\|Event code=US/ELC\|Event group=Examination events OAI\|Response to Election / Restriction Filed\|Event publication date=2011-11-10\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2011-11-29\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2011-11-29\|R4R=112\|RJST=non-final\|Rejected claims 1-20, 33-35 and 38; 33\|Event publication date=2011-11-29\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2011-11-29\|R4R=102b\|RJST=non-final\|Rejected claims 1 and 4\|RJCT=WO200608242\|Event publication date=2011-11-29\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2011-11-29\|R4R=103a\|RJST=non-final\|Rejected claims 1, 3-6, 11 and 16-19; 1-6, 11, 16-20, 33-35 and 38; 1, 3-6, 9-11 and 14-19\|Event publication date=2012-03-29\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2012-03-29\|Event code=US/136G\|Event group=OAO\|Request for Extension of Time - Granted\|Event publication date=2012-05-24\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-07-23\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-09-27\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2012-10-09\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2012-10-09\|R4R=112\|RJST=non-final\|Rejected claims 35\|Event publication date=2012-10-09\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2012-10-09\|R4R=102b\|RJST=non-final\|Rejected claims 38\|RJCT=WO200608242\|Event publication date=2012-10-09\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2012-10-09\|R4R=103a\|RJST=non-final\|Rejected claims 2 and 20; 3; 8; 9 and 10\|RJCT=US4308241\|Event publication date=2013-02-26\|Event code=US/136G\|Event group=OAO\|Request for Extension of Time - Granted\|Event publication date=2013-02-26\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Action Recorded:\|RECD=2013-02-26\|Event publication date=2013-05-21\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2013-05-21\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2013-05-29\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2013-06-17\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2013-06-17\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2013-06-24\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2013-07-10\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2013-07-30\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US08496897\|Publication stage code=B2\|Publication date=2013-07-30\|Standardized publication number=US8496897\|Event publication date=2013-07-30\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 655 Overlap Delays: 50 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 193 Adjustment total: \|Number of days of extension=412\|Event publication date=2013-07-30\|Event code=US/PTA36\|Event group=Extension of term of duration of protection\|PTA 36 Months\|Action Recorded:\|RECD=2013-07-30\|Event publication date=2016-08-09\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2017-01-16\|Event code=US/FPAY\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Fee payment recorded\|Annual fees payment date=2017-01-16\|Year of payment of annual fees=4\|Event publication date=2020-08-11\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|Event publication date=2021-03-22\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2021-07-30\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2021-07-30\|Event publication date=2021-09-06\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2021-09-06\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|Event publication date=2024-08-13\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=11\|(WO2008/101293)\|LEGAL DETAILS FOR WO2008/101293\|Actual or expected expiration date=2010-08-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOAU2008000232\|Application date=2008-02-20\|Standardized application number=2008WO-AU00232\|Event publication date=2008-08-28\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2008101293\|Publication stage code=A1\|Publication date=2008-08-28\|Standardized publication number=WO2008101293\|Event publication date=2010-11-22\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2008217572\|Actual or expected expiration date=2018-09-13\|Legal state=DEAD\|Status=EXPIRED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2008217572\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2008AU-0217572\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2008217572\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2008-08-28\|Publication number in the designated or member state=AU2008217572\|Event publication date=2009-09-18\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2009-10-15\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2018-09-13\|Event code=AU/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=AU\|MEMBER STATE LEGAL DETAILS FOR CA2678800\|Actual or expected expiration date=2019-02-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA2678800\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2008CA-2678800\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA2678800\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2008-08-28\|Publication number in the designated or member state=CA2678800\|Event publication date=2009-08-19\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CA\|Event publication date=2019-04-03\|Event code=CA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR CN101641145\|Actual or expected expiration date=2018-02-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN200880006610\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2008CN-80006610\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN101641145\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2010-02-03\|Publication number in the designated or member state=CN101641145\|Event publication date=2008-02-20\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CN\|Event publication date=2019-02-15\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2009-08-21\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2009-08-21\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP2134449\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP08706115\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member 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state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN6026/DELNP/2009\|Application date in the designated or member state=2009-09-18\|Application number in the designated or member state=2009IN-DN06026\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN6026/DELNP/2009\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-08-26\|Publication number in the designated or member state=IN2009DN06026\|Event publication date=2009-09-18\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|Event publication date=2018-02-26\|Event code=IN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IN\|MEMBER STATE LEGAL DETAILS FOR JP2010519027\|Actual or expected expiration date=2018-08-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=JP Corresponding appl: JP2009550646\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2009JP-0550646\|Corresponding cc:\|Designated or member state=JP Corresponding pat: JP2010519027\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2010-06-03\|Publication number in the designated or member state=JP2010519027\|Event publication date=2009-08-20\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=JP\|Event publication date=2018-08-23\|Event code=JP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=JP\|MEMBER STATE LEGAL DETAILS FOR KR10-2009-0125109\|Actual or expected expiration date=2018-06-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=KR Corresponding appl: KR10-2009-7019662\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2009KR-7019662\|Corresponding cc:\|Designated or member state=KR Corresponding pat: KR10-2009-0125109\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2009-12-03\|Publication number in the designated or member state=KR20090125109\|Event publication date=2009-09-21\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=KR\|Event publication date=2018-06-04\|Event code=KR/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=KR\|MEMBER STATE LEGAL DETAILS FOR US20100021362\|Actual or expected expiration date=2021-09-06\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=US Corresponding appl: US12527608\|Application date in the designated or member state=2008-02-20\|Application number in the designated or member state=2008US-12527608\|Corresponding cc:\|Designated or member state=US Corresponding pat: US20100021362\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2010-01-28\|Publication number in the designated or member state=US20100021362\|Event publication date=2009-09-18\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=US\|Event publication date=2024-08-13\|Event code=US/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=US\|(JP5345954)\|LEGAL DETAILS FOR JP5345954\|Actual or expected expiration date=2018-08-23\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=JP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=JP JP2009550646\|Application date=2008-02-20\|Standardized application number=2009JP-0550646\|Event publication date=2010-06-03\|Event code=JP/A\|Event group=Examination events\|Published application\|Publication country=JP\|Publication number=JP2010519027\|Publication stage code=A\|Publication date=2010-06-03\|Standardized publication number=JP2010519027\|Event publication date=2011-02-08\|Event code=JP/A621\|Event indicator=Pos\|Event group=Examination events\|Written request for application examination\|Japanese intermediate code: A621\|Effective date of the event=2011-02-07\|Event publication date=2012-05-28\|Event code=JP/A977\|Event group=Examination events\|Report on retrieval\|Japanese intermediate code: A971007\|Effective date of the event=2012-05-28\|Event publication date=2012-06-06\|Event 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date=2013-11-20\|Standardized publication number=JP5345954\|Event publication date=2016-08-02\|Event code=JP/R250\|Event indicator=Pos\|Event group=Payment or non-payment notifications Restitution or restoration\|Receipt of annual fees\|Japanese intermediate code: R250\|Event publication date=2017-08-22\|Event code=JP/R250\|Event indicator=Pos\|Event group=Payment or non-payment notifications Restitution or restoration\|Receipt of annual fees\|Japanese intermediate code: R250\|Event publication date=2018-08-23\|Event code=JP/LAPS\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Cancellation because of no payment of annual fees\|(CN101641145)\|LEGAL DETAILS FOR CN101641145\|Actual or expected expiration date=2018-02-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN200880006610\|Application date=2008-02-20\|Standardized application number=2008CN-80006610\|Event publication date=2010-02-03\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN101641145\|Publication stage code=A\|Publication date=2010-02-03\|Standardized publication number=CN101641145\|Event publication date=2010-02-03\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2010-03-24\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2014-05-07\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN101641145\|Publication stage code=B\|Publication date=2014-05-07\|Standardized publication number=CN101641145B\|Event publication date=2014-05-07\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2019-02-15\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee\|Effective date of the event=2018-02-20\|(IN293376)\|LEGAL DETAILS FOR IN293376\|Actual or expected expiration date=2028-02-20\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2009-09-18\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN6026/DELNP/2009\|Application date=2009-09-18\|Standardized application number=2009IN-DN06026\|Event publication date=2011-08-26\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN6026/DELNP/2009\|Publication stage code=A\|Publication date=2011-08-26\|Standardized publication number=IN2009DN06026\|Event publication date=2018-02-26\|Event code=IN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent\|Publication country=IN\|Publication number=IN293376\|Publication stage code=B\|Publication date=2018-02-26\|Standardized publication number=IN-293376\|(CA2678800)\|LEGAL DETAILS FOR CA2678800\|Actual or expected expiration date=2019-02-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2678800\|Application date=2008-02-20\|Standardized application number=2008CA-2678800\|Event publication date=2008-08-28\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2678800\|Publication stage code=A1\|Publication date=2008-08-28\|Standardized publication number=CA2678800\|Event publication date=2013-02-05\|Event code=CA/EEER\|Event indicator=Pos\|Event group=Examination events\|Examination request\|Effective date of the event=2013-01-23\|Event publication date=2015-11-24\|Event code=CA/C\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent (second level)\|Publication country=CA\|Publication number=CA2678800\|Publication stage code=C\|Publication date=2015-11-24\|Standardized publication number=CA2678800\|Event publication date=2019-04-03\|Event code=CA/MKLA\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Lapsed\|Effective date of the event=2019-02-20\|(KR10-1527365)\|LEGAL DETAILS FOR KR10-1527365\|Actual or expected expiration date=2018-06-04\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2008-02-20\|Event code=KR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=KR KR10-2009-7019662\|Application date=2008-02-20\|Standardized application number=2009KR-7019662\|Event publication date=2009-12-03\|Event code=KR/A\|Event group=Examination events\|Published application\|Publication country=KR\|Publication number=KR10-2009-0125109\|Publication stage code=A\|Publication date=2009-12-03\|Standardized publication number=KR20090125109\|Event publication date=2013-01-21\|Event code=KR/A201\|Event group=Examination events\|Request for examination\|Event publication date=2014-03-28\|Event code=KR/E902\|Event indicator=Neg\|Event group=Examination events\|Notification of reason for refusal\|Event publication date=2014-09-26\|Event code=KR/E902\|Event indicator=Neg\|Event group=Examination events\|Notification of reason for refusal\|Event publication date=2015-03-16\|Event code=KR/E701\|Event indicator=Pos\|Event group=Examination events\|Decision to grant or registration\|Event publication date=2015-06-03\|Event code=KR/GRNT\|Event indicator=Pos\|Event group=Examination events\|Written decision to grant\|Event publication date=2015-06-22\|Event code=KR/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent specification\|Publication country=KR\|Publication number=KR10-1527365\|Publication stage code=B1\|Publication date=2015-06-22\|Standardized publication number=KR101527365\|Event publication date=2018-06-04\|Event code=KR/LAPS\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Lapse due to unpaid annual fee\|(AU2008217572)\|LEGAL DETAILS FOR AU2008217572\|Actual or expected expiration date=2018-09-13\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=2008-02-20\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2008217572\|Application date=2008-02-20\|Standardized application number=2008AU-0217572\|Event publication date=2008-08-28\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2008217572\|Publication stage code=A1\|Publication date=2008-08-28\|Standardized publication number=AU2008217572\|Event publication date=2010-02-04\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent proceeded by OPI\|Publication country=AU\|Publication number=AU2008217572\|Publication stage code=B2\|Publication date=2010-02-04\|Standardized publication number=AU2008217572\|Event publication date=2010-06-03\|Event code=AU/FGA\|Event indicator=Pos\|Event group=Event indicating In Force\|Letters patent sealed or granted (standard patent)\|Event publication date=2018-09-13\|Event code=AU/MK14\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent ceased section 143(a) (annual fees not paid) or expired\|(AU2009250983)\|LEGAL DETAILS FOR AU2009250983\|Actual or expected expiration date=2010-12-02\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2009-12-16\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2009250983\|Application date=2009-12-16\|Standardized application number=2009AU-0250983\|Event publication date=2010-01-14\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2009250983\|Publication stage code=A1\|Publication date=2010-01-14\|Standardized publication number=AU2009250983\|Event publication date=2010-12-02\|Event code=AU/MK1\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application lapsed section 142(2)(a) - no request for examination in relevant period	(EP2134449)\|Contracting States: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, GB, IE, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2008/101293)\|ARIPO: GH, GM, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2008/101293)\|EAPO: RU, TJ, BY, MD, AZ, TM, AM, KG, KZ\|(WO2008/101293)\|EPO: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, GB, IE, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2008/101293)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2008/101293)\|National States: PT, HN, HR, HU, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, KM, KN, SV, CH, KP, SY, KR, CN, CO, CR, KZ, CU, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PG, PH, PL	(WO2008/101293)\|IN\|(IN293376)\|IN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=EVho024Sjd+0uo6WVhVzAWkyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP0000000004241227&ekey=2389&xpn=EP2134449&kind=B1	https://register.epo.org/application?number=EP08706115	https://permalink.orbit.com/RenderStaticFirstPage?XPN=ZwTaFI0pS2A1zTc2PWcWRHfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	AU	(WO2008/101293)\|AU	(WO2008/101293)\|NAME=HUNWICK, Richard J. Level 13, 221 Miller Street, North Sydney, New South Wales 2060 , COUNTRY=AU	(EP2134449)\|GB\|(EP2134449)\|GB\|(EP2134449)\|GB\|\|(US20100021362)\|US\|(WO2008/101293)\|AU\|\|\|\|\|(CA2678800)\|CA\|(CA2678800)\|CA\|	(EP2134449)\|NAME=Williams, Richard Andrew Norman;Harrison Goddard Foote 8th Floor 140 London Wall , CITY=London EC2Y 5DN , COUNTRY=GB , REG=100754772\|(EP2134449)\|NAME=Williams, Richard Andrew Norman Harrison Goddard Foote , CITY=40- 43 Chancery LaneLondon WC2A 1JA , COUNTRY=GB , REG=100754772\|(EP2134449)\|NAME=Williams, Richard Andrew Norman;Harrison Goddard Foote 40- 43 Chancery Lane , CITY=LondonWC2A 1JA , COUNTRY=GB , REG=09210841\|(US8496897)\|NAME=Frommer Lawrence & Haug LLP NAME=Santucci Ronald R\|(US20100021362)\|NAME=FROMMER LAWRENCE & HAUG 745 FIFTH AVENUE- 10TH FL. , CITY=NEW YORK , STATE=NY , POSTCODE=10151 , COUNTRY=US\|(WO2008/101293)\|NAME=GRIFFITH HACK Level 29, Northpoint, 100 Miller Street, North Sydney, New South Wales 2060 , COUNTRY=AU\|(JP5345954)\|NAME=YOSHIDA Kenji , REG=100075258NAME=ISHIDA Jun , REG=100096976\|(JP2010519027)\|NAME=YOSHIDA Kenji , REG=100075258NAME=ISHIDA Jun , REG=100096976\|(CN101641145)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(CN101641145)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(CA2678800)\|NAME=MBM INTELLECTUAL PROPERTY LAW LLP , COUNTRY=CA\|(CA2678800)\|NAME=MBM INTELLECTUAL PROPERTY LAW LLP , COUNTRY=CA\|(KR10-2009-0125109)\|NAME=HALLA PATENT & LAW FIRM	(EP2134449)\|AU\|(EP2134449)\|AU\|(EP2134449)\|AU\|(US8496897)\|AU\|(US20100021362)\|AU\|(WO2008/101293)\|AU\|\|\|\|\|\|(IN6026/DELNP/2009)\|AU\|(CA2678800)\|AU\|(CA2678800)\|AU\|\|\|\|\|	(EP2134449)\|NAME=Hunwick, Richard J. 59 Abingdon Road, CITY=Roseville NSW 2069, COUNTRY=AU\|(EP2134449)\|NAME=Hunwick, Richard J. 59 Abingdon Road, CITY=Roseville NSW 2069, COUNTRY=AU\|(EP2134449)\|NAME=Hunwick, Richard J. 221 Miller Street Level 13, CITY=North Sydney, NSW 2060, COUNTRY=AU\|(US8496897)\|NAME=Hunwick Richard J, CITY=North Sydney, COUNTRY=AU\|(US20100021362)\|NAME=Hunwick Richard J., CITY=New South Wales, COUNTRY=AU\|(WO2008/101293)\|NAME=HUNWICK, Richard J. Level 13, 221 Miller Street, North Sydney, New South Wales 2060, COUNTRY=AU\|(JP5345954)\|NAME=Richard Jay Han Wick\|(JP2010519027)\|NAME=Richard Jay Han Wick\|(CN101641145)\|NAME=HUNWICK RICHARD J.\|(CN101641145)\|NAME=HUNWICK RICHARD J.\|(IN293376)\|NAME=HUNWICK RICHARD J\|(IN6026/DELNP/2009)\|NAME=HUNWICK RICHARD J, COUNTRY=AU\|(CA2678800)\|NAME=HUNWICK, RICHARD J., COUNTRY=AU\|(CA2678800)\|NAME=HUNWICK, RICHARD J., COUNTRY=AU\|(KR10-1527365)\|NAME=HUNWICK RICHARD J.\|(KR10-2009-0125109)\|NAME=HUNWICK RICHARD J.\|(AU2008217572)\|NAME=RICHARD J. HUNWICK\|(AU2008217572)\|NAME=RICHARD J. HUNWICK\|(AU2009250983)\|NAME=RICHARD HUNWICK	(WO2008/101293)\|5\|(AU2009250983)\|5\|(IN293376)\|5\|(CA2678800)\|5\|(KR10-1527365)\|5\|(CN101641145)\|5\|(JP5345954)\|5\|(US8496897)\|5\|(EP2134449)\|5\|(AU2008217572)\|5	6	10			(EP2134449)\|WO2008/101293\|(US8496897)\|WO2008/101293\|(JP5345954)\|WO2008/101293\|(CN101641145)\|WO2008/101293\|(IN293376)\|WO2008/101293\|(CA2678800)\|WO2008/101293\|(KR10-1527365)\|WO2008/101293\|(AU2008217572)\|WO2008/101293\|(AU2009250983)\|WO2008/101293		(EP2134449)\|Number of Claims: NCL=21\|Primary examiner: Burkhardt, Thorsten\|\|Primary examiner: Burkhardt, Thorsten\|\|Primary examiner: Burkhardt, Thorsten\|\|(US8496897)\|Number of Claims: NCL=20\|Number of Drawings: NDR=7\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1,18\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=412\|Primary examiner: Silverman Stanley\|Art Unit.: ART =1736\|\|(US20100021362)\|Number of Claims: NCL=32\|Number of Drawings: NDR=8\|Number of Figures: NFG=7\|Independent Claim Number: ICL=1,21,27,28,33\|Number of Independent Claims: NICL=5\|Exemplary Claim Number: ECL=1\|Primary examiner: Silverman Stanley\|Art Unit.: ART =1736\|\|(WO2008/101293)\|Number of Claims: NCL=46\|Extended kind: EXTK=x\|\|(JP5345954)\|Number of Claims: NCL=35\|Number of Pages: NPAGES=22\|Request for examination: REQEXA=false\|\|(JP2010519027)\|Number of Claims: NCL=46\|Number of Pages: NPAGES=28\|Request for examination: REQEXA=false\|\|(CN101641145)\|Number of Claims: NCL=28\|Gazette date: GAZDATE=2014-05-07\|Gazette number: GAZNUM=30-19\|Substantial examination effective date: 20100324 Examination duration: 49 months\|Number of Pages: NPAGES=24\|Primary examiner: Wang Yigang\|Primary examiner: 王义刚\|\|(CN101641145)\|Number of Claims: NCL=46\|Gazette date: GAZDATE=2010-02-03\|Gazette number: GAZNUM=26-05\|Substantial examination effective date: 20100324 Examination duration: 49 months\|Number of Pages: NPAGES=35\|Primary examiner: Wang Yigang\|Primary examiner: 王义刚\|\|(IN293376)\|Number of Claims: NCL=21\|\|(CA2678800)\|Number of Claims: NCL=43\|Number of Pages: NPAGES=44\|\|(CA2678800)\|Number of Claims: NCL=43\|Number of Pages: NPAGES=44\|\|(KR10-1527365)\|Number of Claims: NCL=28\|\|(KR10-2009-0125109)\|Number of Claims: NCL=32\|Number of Pages: NPAGES=26\|\|(AU2008217572)\|Number of Claims: NCL=32\|\|(AU2009250983)\|Number of Claims: NCL=46\|	(US8496897)\|Previous publication: US20100021362 A1 2010-01-28 [US20100021362]\|(AU2009250983)\|Division of: AU2008217572 FDD=2008-02-20 [2008AU-0217572]	(EP2134449)\|ENGLISH (ENG)	(IN-293376)\|Patent\|(CA2678800)\|Patent\|(KR101527365)\|Patent\|(CN101641145B)\|Patent\|(JP5345954)\|Patent\|(US8496897)\|Patent\|(EP2134449)\|Patent\|(IN2009DN06026)\|Patent\|(EP2134449)\|Patent\|(JP2010519027)\|Patent\|(AU2008217572)\|Patent\|(CN101641145)\|Patent\|(US20100021362)\|Patent\|(AU2009250983)\|Patent\|(EP2134449)\|Patent\|(KR20090125109)\|Patent\|(AU2008217572)\|Patent\|(CA2678800)\|Patent\|(WO2008101293)\|Patent	Titre: (EP2134449)\|System, apparatus and method for carbon dioxide sequestration Résumé: (EP2134449)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.	6	Abstract	gpt-4o-mini	yes	The process described involves the use of metal silicate rocks to capture CO₂ and convert it into metal carbonates, which aligns with the topic of enhanced weathering and carbon sequestration.
8	CN202410172022	CN202410172022	CN118134720	110028832	CN118134720 A 2024-06-04 [CN118134720]	2024-02-06	2024-02-06	2024-06-04		(CN118134720)\|2044-02-06	(CN118134720)\|Farmland carbon sequestration and sink increase method, system and equipment based on silicate rock weathering	(CN118134720)\|The invention provides a farmland carbon sequestration and sink increase method, system and equipment based on silicate rock weathering, and the method comprises the steps: obtaining agricultural management basic data; wherein the agricultural management basic data comprises silicate weathering carbon sink data, farmland environment data, soil carbon flux carbon emission data and agricultural management carbon emission data; calculating agricultural production management carbon emission according to the agricultural management basic data; acquiring a preset farmland carbon emission target value; and adjusting farmland management measures according to a preset farmland carbon emission target value and the agricultural production management carbon emission. According to the method, the agricultural production management carbon emission can be calculated, the problem that the farmland carbon emission is unknown after the silicate rock-based carbon sequestration and fertility improvement agent is added is solved, the agricultural production management carbon emission can be accurately estimated, and data support is provided for achieving the carbon emission target. Farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and the preset farmland carbon emission target value.	CHONGQING HUADI ZIHUAN TECHNOLOGY\|CHONGQING INSTITUTE OF GEOLOGY & MINERAL RESOURCES	(CN118134720)\|CHONGQING INSTITUTE OF GEOLOGY AND MINERAL RESOURCES ([CN])\|CHONGQING HUADI ZIHUAN TECHNOLOGY CO., LTD.	MA LEI\|SI HONGTAO\|MAO ZHENG\|WANG CHEN\|LI CHENG\|XU MINGZE\|ZHU DONGXUE\|ZHU DAN\|XU WENXING	(CN118134720)\|MA LEI\|SI HONGTAO\|MAO ZHENG\|WANG CHEN\|LI CHENG\|XU MINGZE\|ZHU DONGXUE\|ZHU DAN\|XU WENXING	(CN118134720)\|YU HONG;CHONGQING ZHI HUI ZHI YUAN INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP)\|Reg. Nb: 50234	(CN118134720)\|Compared with the prior art, the invention has the advantages that: the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation fertilizer-increasing modifier, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for carbon peak and carbon neutralization in the farmland field.\|Those of ordinary skill in the art will appreciate that: the discussion of any of the embodiments above is merely exemplary and is not intended to suggest that the scope of the invention (including the claims) is limited to these examples; the technical features of the above embodiments or in the different embodiments may also be combined within the idea of the invention, the steps may be implemented in any order, and there are many other variations of the different aspects of the embodiments of the invention as described above, which are not provided in detail for the sake of brevity.\|	(CN118134720)\|1. A farmland carbon fixation and sink enhancement method based on silicate rock weathering is characterized by comprising the following steps: Acquiring basic agricultural management data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; calculating an agricultural production management carbon emission amount according to the agricultural management basic data; acquiring a preset farmland carbon emission target value; And adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission.\|	(CN118134720)\|The invention provides a method, a system and equipment for carbon fixation and sink enhancement of farmland based on silicate rock weathering, wherein the method comprises the following steps: acquiring basic agricultural management data; wherein, the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; calculating an agricultural production management carbon emission amount according to the agricultural management basic data; acquiring a preset farmland carbon emission target value; and adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission.\|The invention relates to a farmland carbon fixation and exchange increase method, system and equipment based on silicate rock weathering.\|Therefore, the invention provides a farmland carbon fixation and collection increasing method based on silicate rock weathering, which comprises the steps of firstly obtaining agriculture management basic data, then calculating the agriculture production management carbon emission according to the agriculture management basic data, and then judging whether to adjust farmland management measures according to the agriculture production management carbon emission and a preset farmland carbon emission target value.\|	(CN118134720)\|SILICATE(100,71)\|PRESET FARMLAND CARBON EMISSION(100,28)\|CARBON FIXATION(100,19)\|FARMLAND(100,17)\|FARMLAND CARBON FIXATION(100,7)\|EQUIPMENT(100,4)\|FARMLAND MANAGEMENT(93,7)\|FARMLAND CARBON EMISSION(86,41)\|AGRICULTURAL PRODUCTION MANAGEMENT(84,47)\|AGRICULTURAL MANAGEMENT(69,57)\|CARBON EMISSION(55,135)\|CARBON SEQUESTRATION(55,66)\|FARMLAND ENVIRONMENT DATA(49,16)\|SOIL CARBON FLUX(45,25)\|ADJUSTING FARMLAND MANAGEMENT(45,8)\|PRESET SILICATE WEATHERING(45,3)\|AGRICULTURE PRODUCTION MANAGEMENT(45,2)\|CROP PLANTING(43,13)\|UNCLEAR FARMLAND(43,3)\|UNCLEAR FARMLAND CARBON FIXATION(43,3)\|TARGET VALUE(39,26)\|OBTAINING AGRICULTURE MANAGEMENT(39,1)\|FARMLAND CARBON SEQUESTRATION(37,5)\|CROP ECONOMIC COEFFICIENT(37,4)\|AGRICULTURAL MANAGEMENT DATA(37,3)\|MANAGEMENT REVISION MODULE(36,3)\|UNKNOWN FARMLAND CARBON EMISSION(36,1)\|CARBON SEQUESTRATION DATA(35,24)\|FARMLAND MANAGEMENT MEASURE(35,4)\|CARBON EMISSION DATA(34,41)\|PRESET CROP(34,8)\|BASIC AGRICULTURAL MANAGEMENT DATA(34,3)\|SOIL CARBON EMISSION(33,16)\|TRAINING(32,16)\|FERTILIZER INCREASING MODIFIER(32,1)\|CARBON SEQUESTRATION MODEL(31,14)\|AGRICULTURAL MANAGEMENT BASIC DATA(31,4)\|EMISSION CALCULATION MODULE(30,2)\|CROP SOIL TEXTURE(29,3)\|AGRICULTURAL MANAGEMENT ACQUISITION(29,2)\|SILICATE WEATHERED CARBON SEQUESTRATION(29,1)\|INPUTTING SILICATE(27,3)\|ROCK CARBON FIXATION(27,2)\|DATA BASIS(26,9)\|CARBON NEUTRALIZATION(26,3)\|AGRICULTURE MANAGEMENT(26,1)\|AGRICULTURAL MANAGEMENT BASE DATA(25,14)\|AGRICULTURAL MANAGEMENT CARBON EMISSION(25,12)\|AGRICULTURE MANAGEMENT BASIC DATA(24,1)\|TECHNICAL FEATURE(24,1)\|IRRIGATION CARBON EMISSION COEFFICIENT(23,3)\|OBTAINING CARBON PLANTING(23,3)\|PESTICIDE CARBON EMISSION COEFFICIENT(23,3)\|PRESET AGRICULTURAL MANAGEMENT(23,3)\|UNCLEAR CARBON EMISSION(23,3)\|CARBON SINK MODEL(22,14)\|AGRICULTURAL PRODUCTION MANAGEMENT CALCULATION(22,2)\|BREVITY(22,1)\|EXOGENOUS SILICATE ROCK ADDITION(21,9)\|O TH CULTIVATION(21,6)\|PRESET TARGET(21,2)\|CROP FARMLAND AREA(20,3)\|SILICATE PREDICTION MODEL(20,3)\|PRODUCTION MANAGEMENT(20,2)\|NETWORK SOURCE(19,12)\|CROP GROWTH CARBON SINK(19,3)\|TARGET ACQUISITION MODULE(19,2)\|CALCULATED AGRICULTURAL PRODUCTION MANAGEMENT(18,3)\|CARBON PEAK(18,3)\|CARBON EMISSION TARGET(18,1)\|MOISTURE CONTENT(17,4)\|CARBON SINK DATA(15,17)\|RAINFALL(14,4)\|N TH PESTICIDE(14,3)\|PRESET CARBON EMISSION(14,3)\|INPUTTING CARBON EMISSION DATA(14,1)\|UNUTILIZED MINE TAILING(14,1)\|GROUND(13,5)\|RANDOM FOREST(13,5)\|CROP CARBON FLUX DATA(13,3)\|GROWTH PERIOD(13,3)\|SUPPORTING DATA(12,4)\|CARBON EMISSION MODEL(12,3)\|SILICATE ROCK PARTICLE SIZE(11,4)\|FERTILIZER ENHANCEMENT MODIFIER(11,1)\|SILICATE ROCK WEATHERING(11,1)\|AGRICULTURAL MACHINE CARBON EMISSION(10,5)\|CHEMICAL FERTILIZER CARBON EMISSION(10,4)\|NEURAL NETWORK(10,4)\|ROOT CAP RATIO(10,4)\|SINK INCREASING DATA(10,4)\|DATA ACQUISITION MODULE(10,3)\|FARMLAND FIELD(9,3)\|NONLINEAR FUNCTION MODEL(9,3)\|COMPREHENSIVE GREEN TRANSFORMATION(8,1)\|ORGANIC SUBSTANCE(7,3)\|FARMLAND CULTIVATION CARBON EMISSION(7,1)\|REALIZING FARMLAND(7,1)\|SYNERGY PROMOTION(7,1)\|COMMUNICATION INTERFACE(6,4)\|ACCELERATE SILICATE(6,1)\|AM VM M(6,1)\|FARMLAND SOIL(6,1)\|POTASSIUM FELDSPAR(6,1)\|SOIL ECOSYSTEM(6,1)\|VEGETATION RECOVERY(6,1)\|AGRICULTURAL MANAGEMENT MEASURE DATA(5,3)\|COMMUNICATION MODULE(5,2)\|CROP PLANTED CARBON SEQUESTRATION(5,1)\|DISTRIBUTED SCENARIO(5,1)\|DISTRIBUTED SCENE(5,1)\|ECOLOGICAL ENVIRONMENT(5,1)\|ECONOMY DEVELOPMENT(5,1)\|ENERGY UTILIZATION IMPORTANCE(5,1)\|QUICK CALCULATION(5,1)\|AGRICULTURAL MACHINE FUEL INFORMATION(4,2)\|PRECIPITATION(4,2)\|AL UL L(4,1)\|AUTOMATIC CALCULATION(4,1)\|COMMUNICATION INTERACTION(4,1)\|CROP GROWTH CONDITION(4,1)\|CULTIVATION MODE(4,1)\|ECOLOGICAL CIVILIZATION CONSTRUCTION(4,1)\|ENHANCED SILICATE(4,1)\|EQUIVALENT SUBSTITUTION(4,1)\|ESTIMATED AGRICULTURAL PRODUCTION MANAGEMENT(4,1)\|IDENTIFICATION MODEL(4,1)\|NEGATIVE EMISSION(4,1)\|OBTAINING AGRICULTURAL MANAGEMENT(4,1)\|ORDINARY MEANING(4,1)\|POSITIONAL RELATIONSHIP(4,1)\|PRESET SOIL CARBON FLUX(4,1)\|	(CN118134720)\|1. A farmland carbon fixation and sink enhancement method based on silicate rock weathering is characterized by comprising the following steps:\| Acquiring basic agricultural management data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \| calculating an agricultural production management carbon emission amount according to the agricultural management basic data; \| acquiring a preset farmland carbon emission target value; \| And adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|2. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering of claim 1, wherein the calculating the agricultural production management carbon emissions from the agricultural management base data comprises:\| Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \| Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \| obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \| obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \| And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|3. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 2, wherein the training process of the silicate-weathered carbon sequestration model comprises:\| Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \| the carbon sink model for the weathering of the preset silicate comprises the following components: \|Wx=F(x,y,q,d)\| Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|4. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 2, wherein the training process of the carbon sequestration model for crop planting comprises:\| Obtaining carbon planting and sink increasing data according to the farmland environment data; \| The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \| wherein, the carbon sequestration model for the preset crop planting comprises: \|Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\| Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|5. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 2, wherein the training process of the carbon emission model of the soil carbon flux comprises:\| Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \| Wherein, the carbon emission model of the preset soil carbon flux comprises: \|Fp=∑Ti·Ai,ki·ti\| Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|6. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering of claim 2, wherein the training process of the carbon emission model for agricultural management comprises:\| The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \| wherein, the carbon emission model of preset agricultural management includes: \|Mp=M1+M2+M3+M4\|M1=∑Al·Ul·αl\|M2=∑Am·Vm·αm\|M3=∑An·Wn·αn\|M4=∑Ao·αo\| Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|7. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 2, wherein the silicate rock weathering farmland carbon emission prediction model comprises:\|S=Mp+Fp-Wx-Zx\| Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|8. The method for carbon sequestration and sequestration in farmlands based on silicate rock weathering according to claim 1, wherein the adjusting farmland management measures according to the preset target value of farmland carbon emission and the agricultural production management carbon emission comprises:\| judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \| and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|9. A silicate-based weathered farmland carbon sequestration and sequestration system for implementing a silicate-based weathered farmland carbon sequestration and sequestration method according to claims 1-8, comprising:\| the data acquisition module is used for acquiring the agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \| An emission calculation module for calculating an agricultural production management carbon emission amount according to the agricultural management base data; \| the target acquisition module is used for acquiring a preset farmland carbon emission target value; \| And the management revision module is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|10. An apparatus comprising a memory, a processor and a computer program stored on the memory and executable on the processor, wherein the processor implements the steps of the method of any one of claims 1 to 8 when the computer program is executed.	(CN118134720)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to a farmland carbon fixation and exchange increase method, system and equipment based on silicate rock weathering.\|BACKGROUND ART\|[0002] With the development of economy, the importance of effective energy utilization, environmental pollution reduction and climate change is increasingly highlighted. The ecological civilization construction of China enters a key period for promoting the synergy of pollution reduction and carbon reduction, promoting the comprehensive green transformation of economic and social development and realizing the change of the quality improvement of ecological environment from variable quantity to variable quality.\|[0003] Enhanced silicate rock weathering is a negative emission technique based on the geochemical principle that aims to accelerate the silicate rock chemical weathering process by adding silicate rock powder to farms or forests to fix more atmospheric CO 2 in a shorter time. The potassium feldspar mineral resources in China are rich, the reserves are huge, the grade is excellent, and a large amount of unutilized mine tailings and alkali silicate waste materials exist, so that the potential of removing the atmospheric CO 2 by enhancing the weathering of silicate rock is huge. At present, a calculation method for carbon emission of soil after silicate rock addition is not available, and a method for carbon fixation and sink increase of soil based on silicate rock weathering is not available.\|DISCLOSURE\|Disclosure of Invention\|[0004] Based on the above, it is necessary to provide a method, a system and a device for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering.\|[0005] A farmland carbon fixation and exchange increase method based on silicate rock weathering comprises the following steps:\|[0006] Acquiring basic agricultural management data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0007] calculating an agricultural production management carbon emission amount according to the agricultural management basic data; \|[0008] acquiring a preset farmland carbon emission target value; \|[0009] And adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|[0010] In one embodiment, calculating the agricultural production management carbon emissions from the agricultural management basis data includes:\|[0011] Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \|[0012] Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \|[0013] obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \|[0014] obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \|[0015] And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|[0016] In one embodiment, the training process for a silicate weathered carbon sink model includes:\|[0017] Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \|[0018] the carbon sink model for the weathering of the preset silicate comprises the following components: \|[0019] Wx=F(x,y,q,d)\|[0020] Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|[0021] In one of the embodiments of the present invention,\|[0022] The training process of the carbon sequestration model for crop planting comprises the following steps:\|[0023] Obtaining carbon planting and sink increasing data according to the farmland environment data; \|[0024] The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \|[0025] wherein, the carbon sequestration model for the preset crop planting comprises: \|[0026] Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\|[0027] Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|[0028] In one embodiment, the training process of the carbon emission model of the soil carbon flux comprises:\|[0029] Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \|[0030] Wherein, the carbon emission model of the preset soil carbon flux comprises: \|[0031] Fp=∑Ti·Ai,ki·ti\|[0032] Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|[0033] In one embodiment, the training process for an agricultural managed carbon emission model includes:\|[0034] The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \|[0035] wherein, the carbon emission model of preset agricultural management includes: \|[0036] Mp=M1+M2+M3+M4\|[0037] M1=∑Al·Ul·αl\|[0038] M2=∑Am·Vm·αm\|[0039] M3=∑An·Wn·αn\|[0040] M4=∑Ao·αo\|[0041] Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|[0042] In one embodiment, a silicate-weathered farmland carbon emission prediction model includes:\|[0043] S=Mp+Fp-Wx-Zx\|[0044] Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|[0045] In one embodiment, adjusting the farmland management measure according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount includes:\|[0046] judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \|[0047] and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|[0048] A farmland carbon sequestration and sequestration system based on silicate rock weathering is used for realizing the farmland carbon sequestration and sequestration method based on silicate rock weathering, and comprises the following steps:\|[0049] the data acquisition module is used for acquiring the agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0050] An emission calculation module for calculating an agricultural production management carbon emission amount according to the agricultural management base data; \|[0051] the target acquisition module is used for acquiring a preset farmland carbon emission target value; \|[0052] And the management revision module is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|[0053] An apparatus comprising a memory, a processor and a computer program stored on the memory and executable on the processor, the processor implementing the steps of a silicate rock weathering based farmland carbon sequestration and sequestration method as described in the various embodiments above when the program is executed.\|[0054] Compared with the prior art, the invention has the advantages that: the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation fertilizer-increasing modifier, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for carbon peak and carbon neutralization in the farmland field. Meanwhile, farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and a preset farmland carbon emission target value, and the aim of low carbon emission of agricultural production is achieved.\|DRAWINGS DESCRIPTION\|[0055] FIG. 1 is a schematic flow diagram of a method for carbon sequestration and sequestration in a farmland based on silicate rock weathering in an embodiment;\|[0056] FIG. 2 is a schematic diagram of a system for carbon sequestration and sequestration in a farmland based on silicate rock weathering in accordance with an embodiment; \|[0057] Fig. 3 is a schematic diagram of the internal structure of the apparatus in one embodiment. \|INVENTION MODE\|Detailed Description\|[0058] Before proceeding with the description of the embodiments of the present invention, the general inventive concept will be described as follows:\|[0059] The invention is mainly developed in the silicate rock farmland improvement process, and at present, a calculation method for carbon emission of soil after silicate rock addition is not available, and a method for carbon fixation and sink enhancement of soil based on silicate rock weathering is not available. \|[0060] Therefore, the invention provides a farmland carbon fixation and collection increasing method based on silicate rock weathering, which comprises the steps of firstly obtaining agriculture management basic data, then calculating the agriculture production management carbon emission according to the agriculture management basic data, and then judging whether to adjust farmland management measures according to the agriculture production management carbon emission and a preset farmland carbon emission target value. The invention realizes quick calculation of farmland carbon emission of different types of farmland soil, silicate rock types, silicate rock addition amount, silicate rock particle size and different cultivation modes, and provides decision support for farmland management.\|[0061] Having described the general inventive concept, the present invention will be further described in detail with reference to the accompanying drawings by way of specific embodiments thereof, in order to make the objects, technical solutions and advantages of the present invention more apparent.\|[0062] It should be noted that unless otherwise defined, technical or scientific terms used in one or more embodiments of the present specification should be given the ordinary meaning as understood by one of ordinary skill in the art to which the present invention pertains. The use of the terms "first," "second," and the like in one or more implementations of the present description does not denote any order, quantity, or importance, but rather the terms "first," "second," and the like are used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that elements or items preceding the word are included in the element or item listed after the word and equivalents thereof, but does not exclude other elements or items. The terms "connected" or "connected," and the like, are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", etc. are used merely to indicate relative positional relationships, which may also be changed when the absolute position of the object to be described is changed.\|[0063] For convenience of understanding, the terms involved in the embodiments of the present invention are explained below:\|[0064] Carbon sink is the process, activity or mechanism of absorbing carbon dioxide in the atmosphere by means of tree planting, vegetation recovery and the like, thereby reducing the concentration of greenhouse gases in the atmosphere. Land ecosystems such as forests, grasslands, wetlands, farmlands, deserts, cities and the like and marine ecosystems are important carbon sinks. \|[0065] Carbon sequestration and sequestration means that the carbon dioxide absorption and storage capacity of an ecosystem are increased by various means and measures, thereby reducing the concentration of carbon dioxide in the atmosphere.\|[0066] In one embodiment, as shown in fig. 1, there is provided a method for carbon sequestration and sequestration in a farmland based on silicate rock weathering, comprising the steps of:\|[0067] Step S101, obtaining agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux, and carbon emission data for agricultural management. \|[0068] Specifically, agricultural management base data is acquired, the agricultural management base data including: carbon sink data based on silicate weathering, farmland environment data based on crop planting, carbon emission data based on soil carbon flux, and carbon emission data based on agricultural management. Wherein the carbon sink data based on silicate weathering comprises: silicate rock type, particle size, precipitation, application amount, weathered carbon sequestration data and the like; the farmland environment data based on crop planting includes: crop growth conditions, climate, weather, air quality, temperature and humidity and the like; carbon emission data based on soil carbon flux includes: carbon flux data, field area data, crop planting time and the like of different crop planting based on exogenous silicate rock addition; carbon emission data based on agricultural management includes: agricultural machine usage data, various kinds of agricultural machine fuel information, agricultural management measure data, and the like.\|[0069] Step S102, calculating the agricultural production management carbon emission amount according to the agricultural management basic data.\|[0070] Specifically, the estimated agricultural production management carbon emission amount can be calculated from the agricultural management base data.\|[0071] On this basis, calculating the agricultural production management carbon emission amount from the agricultural management basis data includes:\|[0072] Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \|[0073] Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \|[0074] obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \|[0075] obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \|[0076] And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|[0077] Specifically, a silicate-weathered carbon sink model based on silicate-weathered silicate is built, a crop-planted carbon sequestration model based on crop planting, a soil carbon flux carbon emission model based on soil respiration and an agricultural management carbon emission model based on agricultural production management are built, a silicate-weathered farmland carbon emission prediction model is built, and the agricultural production management carbon emission amount is obtained through the silicate-weathered farmland carbon emission prediction model.\|[0078] In the embodiment, the carbon emission amount of agricultural production management is calculated by establishing a plurality of models, so that the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation and fertilizer enhancement modifier are solved, the carbon emission amount of agricultural production management can be estimated accurately, and data support is provided for ' carbon peak and ' carbon neutralization ' in the farmland field.\|[0079] On the basis, the training process of the silicate weathered carbon sink model comprises the following steps:\|[0080] Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \|[0081] the carbon sink model for the weathering of the preset silicate comprises the following components: \|[0082] Wx=F(x,y,q,d)\|[0083] Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|[0084] Specifically, a carbon sink model of pre-set silicate weathering based on a random forest algorithm is constructed, W x =f (x, y, q, d). Wherein, F () represents a nonlinear function model of silicate-decomposed carbon sequestration and silicate type, rainfall, silicate application, silicate grain size constructed by random forest algorithm. And training a carbon sink model of the preset silicate weathering through the training data set to obtain the carbon sink model of the silicate weathering which meets the expectations. And acquiring silicate rock type, particle size, precipitation, application amount and weathered carbon fixation data, and calculating the carbon dioxide fixation amount generated by silicate rock weathering, namely the carbon sink amount generated by exogenous silicate rock addition.\|[0085] On the basis, the training process of the carbon sequestration model for crop planting comprises the following steps:\|[0086] Obtaining carbon planting and sink increasing data according to the farmland environment data; \|[0087] The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \|[0088] wherein, the carbon sequestration model for the preset crop planting comprises: \|[0089] Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\|[0090] Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|[0091] Specifically, farmland environment data are obtained, and carbon planting and collection increasing data of a target area are obtained through the existing identification model. Wherein, the carbon planting and sink increasing data comprises: crop type information and plant type information, crop weight information, moisture content of harvested part of crops, root cap ratio of crops and economic coefficient of crops.\|[0092] And constructing a carbon sequestration model Z x=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi for the preset crop planting based on the crop planting, training the carbon sequestration model for the preset crop planting through a training data set to obtain a carbon sequestration model which accords with the expected crop planting, and calculating the carbon sequestration amount generated by the crop growth according to the carbon sequestration data.\|[0093] On the basis, the training process of the carbon emission model of the soil carbon flux comprises the following steps:\|[0094] Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \|[0095] Wherein, the carbon emission model of the preset soil carbon flux comprises: \|[0096] Fp=∑Ti·Ai,ki·ti\|[0097] Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|[0098] Specifically, a multiple regression relation between measured carbon flux data and crop planting types and soil textures is constructed, a carbon emission model of the preset soil carbon flux based on the crop types and the soil textures is determined, F p=∑Ti·Ai,ki·ti, and training of the carbon emission model of the preset soil carbon flux is carried out through a training data set, so that a carbon emission model which accords with expected soil carbon flux is obtained. And obtaining carbon flux data, field area data and crop planting time based on different crop planting of exogenous silicate rock addition, and calculating to obtain the carbon emission of the soil.\|[0099] In the embodiment, based on the BP neural network, a multiple regression relation between actually measured exogenous silicate rock added carbon flux data and crop planting types and soil textures is constructed, and the automatic calculation of the carbon emission of the soil can be realized by operating the constructed carbon emission model of the soil carbon flux.\|[0100] On this basis, the training process of the carbon emission model of agricultural management comprises the following steps:\|[0101] The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \|[0102] wherein, the carbon emission model of preset agricultural management includes: \|[0103] Mp=M1+M2+M3+M4\|[0104] M1=∑Al·Ul·αl\|[0105] M2=∑Am·Vm·αm\|[0106] M3=∑An·Wn·αn\|[0107] M4=∑Ao·αo\|[0108] Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|[0109] Specifically, the use data of the agricultural machine is obtained, the agricultural management carbon emission is calculated by combining the agricultural management measure data, and the agricultural production carbon emission information is obtained. Various agricultural machine usage data include: fuel oil information of various kinds of agricultural machines, time length information of various kinds of agricultural machines, power information of various kinds of agricultural machines, and use quantity information of various kinds of agricultural machines; acquiring carbon emission factor information of various fuels based on the fuel information of various agricultural machines, and multiplying the carbon emission factor information of various fuels, the power information of various agricultural machines, the time-length information of various agricultural machines and the use quantity information of various agricultural machines to obtain the carbon emission quantity of the agricultural machines; obtaining chemical fertilizer use information and pesticide use information according to the agricultural management measure data, obtaining chemical fertilizer carbon emission factor information of various types and pesticide carbon emission factor information of various types based on the chemical fertilizer use information and the pesticide use information, calculating the product of the chemical fertilizer use information and the carbon emission factor of the corresponding chemical fertilizer type as chemical fertilizer carbon emission amount, and calculating the product of the pesticide use information and the carbon emission factor of the corresponding pesticide type as pesticide carbon emission amount; calculating the product of the cultivation and irrigation use information and the carbon emission factors of the corresponding modes as the carbon emission amount of farmland cultivation and irrigation; and combining the carbon emission of the agricultural machine, the carbon emission of the fertilizer, the carbon emission of the pesticide and the carbon emission of farmland cultivation and irrigation to obtain the carbon emission of agricultural management.\|[0110] In the embodiment, carbon emission calculation including the use of agricultural machinery, the use of chemical fertilizers and the application of pesticides in the whole agricultural management process can be realized.\|[0111] On the basis, the farmland carbon emission prediction model for silicate rock weathering comprises the following steps:\|[0112] S=Mp+Fp-Wx-Zx\|[0113] Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|[0114] Specifically, a farmland carbon emission prediction model s=m p+Fp-Wx-Zx based on silicate rock weathering is constructed, and the agricultural production management carbon emission amount is calculated according to the model.\|[0115] Step S103, obtaining a preset farmland carbon emission target value.\|[0116] Specifically, a preset farmland carbon emission target value is set manually, and the preset farmland carbon emission target value is obtained.\|[0117] In this embodiment, a preset target carbon emission value of the farmland is set, and the optimal silicate addition amount and the optimal farmland management measure of the farmland can be determined according to the preset target carbon emission value of the farmland.\|[0118] And step S104, adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount.\|[0119] The farmland management measure adjusting method according to the preset farmland carbon emission target value and the agricultural production management carbon emission comprises the following steps:\|[0120] judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \|[0121] and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|[0122] Specifically, according to the agricultural production management carbon emission calculated by the silicate-weathered farmland carbon emission prediction model, judging whether the agricultural production management carbon emission is greater than a preset farmland carbon emission target value, if not, adjusting the silicate addition amount or changing the addition type and particle size and optimizing farmland management measures.\|[0123] The farmland carbon fixation and collection increasing method based on silicate rock weathering provided by the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after silicate rock carbon fixation and fertilizer increase modifier is added, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for ' carbon peak and ' carbon neutralization ' in the farmland field. Meanwhile, farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and a preset farmland carbon emission target value, and the aim of low carbon emission of agricultural production is achieved.\|[0124] It should be noted that, the method of the embodiment of the present invention may be performed by a single device, for example, a computer or a server. The method of the embodiment can also be applied to a distributed scene, and is completed by mutually matching a plurality of devices. In the case of such a distributed scenario, one of the devices may perform only one or more steps of the method of an embodiment of the present invention, the devices interacting with each other to accomplish the method.\|[0125] It should be noted that the foregoing describes some embodiments of the present invention. Other embodiments are within the scope of the following claims. In some cases, the actions or steps recited in the claims may be performed in a different order than in the embodiments described above and still achieve desirable results. In addition, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In some embodiments, multitasking and parallel processing are also possible or may be advantageous.\|[0126] Based on the same inventive concept, the invention also provides a farmland carbon fixation and exchange increasing system based on silicate rock weathering, which corresponds to the method of any embodiment.\|[0127] Referring to fig. 2, the farmland carbon sequestration and sequestration system based on silicate rock weathering includes:\|[0128] A data acquisition module 201, configured to acquire agricultural management base data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0129] An emissions calculation module 202 for calculating an agricultural production management carbon emissions based on the agricultural management base data; \|[0130] a target obtaining module 203, configured to obtain a preset target value of carbon emission in a farmland; \|[0131] and the management revision module 204 is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount. \|[0132] For convenience of description, the above system is described as being functionally divided into various modules, respectively. Of course, the functions of each module may be implemented in the same piece or pieces of software and/or hardware when implementing the present invention.\|[0133] The system of the above embodiment is used for implementing a corresponding method for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering in any of the foregoing embodiments, and has the beneficial effects of the corresponding method embodiments, which are not described herein.\|[0134] Based on the same inventive concept, the invention also provides equipment corresponding to the method in any embodiment, which comprises a memory, a processor and a computer program stored on the memory and capable of running on the processor, wherein the processor realizes the farmland carbon fixation and exchange increasing method based on silicate rock weathering in any embodiment when executing the program.\|[0135] Fig. 3 shows a more specific hardware architecture of the device provided in this embodiment, where the device may include: a processor 1010, a memory 1020, an input/output interface 1030, a communication interface 1040, and a bus 1050. Wherein processor 1010, memory 1020, input/output interface 1030, and communication interface 1040 implement communication connections therebetween within the device via a bus 1050.\|[0136] The processor 1010 may be implemented by a general-purpose CPU (Central Processing Unit ), a microprocessor, an Application SPECIFIC INTEGRATED Circuit (ASIC), or one or more integrated circuits, etc. for executing related programs to implement the technical solutions provided in the embodiments of the present disclosure.\|[0137] The Memory 1020 may be implemented in the form of ROM (Read Only Memory), RAM (Random Access Memory ), static storage, dynamic storage, etc. Memory 1020 may store an operating system and other application programs, and when the embodiments of the present specification are implemented in software or firmware, the associated program code is stored in memory 1020 and executed by processor 1010.\|[0138] The input/output interface 1030 is used to connect with an input/output module for inputting and outputting information. The input/output module may be configured as a component in a device (not shown) or may be external to the device to provide corresponding functionality. Wherein the input devices may include a keyboard, mouse, touch screen, microphone, various types of sensors, etc., and the output devices may include a display, speaker, vibrator, indicator lights, etc.\|[0139] Communication interface 1040 is used to connect communication modules (not shown) to enable communication interactions of the present device with other devices. The communication module may implement communication through a wired manner (such as USB, network cable, etc.), or may implement communication through a wireless manner (such as mobile network, WIFI, bluetooth, etc.).\|[0140] Bus 1050 includes a path for transferring information between components of the device (e.g., processor 1010, memory 1020, input/output interface 1030, and communication interface 1040).\|[0141] It should be noted that although the above-described device only shows processor 1010, memory 1020, input/output interface 1030, communication interface 1040, and bus 1050, in an implementation, the device may include other components necessary to achieve proper operation. Furthermore, it will be understood by those skilled in the art that the above-described apparatus may include only the components necessary to implement the embodiments of the present description, and not all the components shown in the drawings.\|[0142] The device of the above embodiment is used for implementing a corresponding method for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering in any of the foregoing embodiments, and has the beneficial effects of the corresponding method embodiment, which are not described herein.\|[0143] Those of ordinary skill in the art will appreciate that: the discussion of any of the embodiments above is merely exemplary and is not intended to suggest that the scope of the invention (including the claims) is limited to these examples; the technical features of the above embodiments or in the different embodiments may also be combined within the idea of the invention, the steps may be implemented in any order, and there are many other variations of the different aspects of the embodiments of the invention as described above, which are not provided in detail for the sake of brevity.\|[0144] Any process or method descriptions in flow charts or otherwise described herein may be understood as representing modules, segments, or portions of code which include one or more executable instructions for implementing specific logical functions or steps of the process, and further implementations are included within the scope of the preferred embodiment of the present invention in which functions may be executed out of order from that shown or discussed, including substantially concurrently or in reverse order, depending on the functionality involved, as would be understood by those reasonably skilled in the art of the present invention.\|[0145] Where specific details are set forth in order to describe example embodiments of the invention, it should be apparent to one skilled in the art that embodiments of the invention can be practiced without, or with variation of, these specific details. Accordingly, the description is to be regarded as illustrative in nature and not as restrictive.\|[0146] While the invention has been described in conjunction with specific embodiments thereof, many alternatives, modifications, and variations of those embodiments will be apparent to those skilled in the art in light of the foregoing description.\|[0147] The present embodiments are intended to embrace all such alternatives, modifications and variances which fall within the broad scope of the appended claims. Therefore, any omissions, modifications, equivalent substitutions, improvements, and the like, which are within the spirit and principles of the embodiments of the invention, are intended to be included within the scope of the invention.	(CN118134720)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to a farmland carbon fixation and exchange increase method, system and equipment based on silicate rock weathering.\|BACKGROUND ART\|[0002] With the development of economy, the importance of effective energy utilization, environmental pollution reduction and climate change is increasingly highlighted. The ecological civilization construction of China enters a key period for promoting the synergy of pollution reduction and carbon reduction, promoting the comprehensive green transformation of economic and social development and realizing the change of the quality improvement of ecological environment from variable quantity to variable quality.\|[0003] Enhanced silicate rock weathering is a negative emission technique based on the geochemical principle that aims to accelerate the silicate rock chemical weathering process by adding silicate rock powder to farms or forests to fix more atmospheric CO 2 in a shorter time. The potassium feldspar mineral resources in China are rich, the reserves are huge, the grade is excellent, and a large amount of unutilized mine tailings and alkali silicate waste materials exist, so that the potential of removing the atmospheric CO 2 by enhancing the weathering of silicate rock is huge. At present, a calculation method for carbon emission of soil after silicate rock addition is not available, and a method for carbon fixation and sink increase of soil based on silicate rock weathering is not available.\|DISCLOSURE\|Disclosure of Invention\|[0004] Based on the above, it is necessary to provide a method, a system and a device for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering.\|[0005] A farmland carbon fixation and exchange increase method based on silicate rock weathering comprises the following steps:\|[0006] Acquiring basic agricultural management data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0007] calculating an agricultural production management carbon emission amount according to the agricultural management basic data; \|[0008] acquiring a preset farmland carbon emission target value; \|[0009] And adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|[0010] In one embodiment, calculating the agricultural production management carbon emissions from the agricultural management basis data includes:\|[0011] Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \|[0012] Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \|[0013] obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \|[0014] obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \|[0015] And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|[0016] In one embodiment, the training process for a silicate weathered carbon sink model includes:\|[0017] Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \|[0018] the carbon sink model for the weathering of the preset silicate comprises the following components: \|[0019] Wx=F(x,y,q,d)\|[0020] Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|[0021] In one of the embodiments of the present invention,\|[0022] The training process of the carbon sequestration model for crop planting comprises the following steps:\|[0023] Obtaining carbon planting and sink increasing data according to the farmland environment data; \|[0024] The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \|[0025] wherein, the carbon sequestration model for the preset crop planting comprises: \|[0026] Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\|[0027] Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|[0028] In one embodiment, the training process of the carbon emission model of the soil carbon flux comprises:\|[0029] Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \|[0030] Wherein, the carbon emission model of the preset soil carbon flux comprises: \|[0031] Fp=∑Ti·Ai,ki·ti\|[0032] Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|[0033] In one embodiment, the training process for an agricultural managed carbon emission model includes:\|[0034] The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \|[0035] wherein, the carbon emission model of preset agricultural management includes: \|[0036] Mp=M1+M2+M3+M4\|[0037] M1=∑Al·Ul·αl\|[0038] M2=∑Am·Vm·αm\|[0039] M3=∑An·Wn·αn\|[0040] M4=∑Ao·αo\|[0041] Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|[0042] In one embodiment, a silicate-weathered farmland carbon emission prediction model includes:\|[0043] S=Mp+Fp-Wx-Zx\|[0044] Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|[0045] In one embodiment, adjusting the farmland management measure according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount includes:\|[0046] judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \|[0047] and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|[0048] A farmland carbon sequestration and sequestration system based on silicate rock weathering is used for realizing the farmland carbon sequestration and sequestration method based on silicate rock weathering, and comprises the following steps:\|[0049] the data acquisition module is used for acquiring the agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0050] An emission calculation module for calculating an agricultural production management carbon emission amount according to the agricultural management base data; \|[0051] the target acquisition module is used for acquiring a preset farmland carbon emission target value; \|[0052] And the management revision module is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission. \|[0053] An apparatus comprising a memory, a processor and a computer program stored on the memory and executable on the processor, the processor implementing the steps of a silicate rock weathering based farmland carbon sequestration and sequestration method as described in the various embodiments above when the program is executed.\|[0054] Compared with the prior art, the invention has the advantages that: the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation fertilizer-increasing modifier, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for carbon peak and carbon neutralization in the farmland field. Meanwhile, farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and a preset farmland carbon emission target value, and the aim of low carbon emission of agricultural production is achieved.\|DRAWINGS DESCRIPTION\|[0055] FIG. 1 is a schematic flow diagram of a method for carbon sequestration and sequestration in a farmland based on silicate rock weathering in an embodiment;\|[0056] FIG. 2 is a schematic diagram of a system for carbon sequestration and sequestration in a farmland based on silicate rock weathering in accordance with an embodiment; \|[0057] Fig. 3 is a schematic diagram of the internal structure of the apparatus in one embodiment. \|INVENTION MODE\|Detailed Description\|[0058] Before proceeding with the description of the embodiments of the present invention, the general inventive concept will be described as follows:\|[0059] The invention is mainly developed in the silicate rock farmland improvement process, and at present, a calculation method for carbon emission of soil after silicate rock addition is not available, and a method for carbon fixation and sink enhancement of soil based on silicate rock weathering is not available. \|[0060] Therefore, the invention provides a farmland carbon fixation and collection increasing method based on silicate rock weathering, which comprises the steps of firstly obtaining agriculture management basic data, then calculating the agriculture production management carbon emission according to the agriculture management basic data, and then judging whether to adjust farmland management measures according to the agriculture production management carbon emission and a preset farmland carbon emission target value. The invention realizes quick calculation of farmland carbon emission of different types of farmland soil, silicate rock types, silicate rock addition amount, silicate rock particle size and different cultivation modes, and provides decision support for farmland management.\|[0061] Having described the general inventive concept, the present invention will be further described in detail with reference to the accompanying drawings by way of specific embodiments thereof, in order to make the objects, technical solutions and advantages of the present invention more apparent.\|[0062] It should be noted that unless otherwise defined, technical or scientific terms used in one or more embodiments of the present specification should be given the ordinary meaning as understood by one of ordinary skill in the art to which the present invention pertains. The use of the terms "first," "second," and the like in one or more implementations of the present description does not denote any order, quantity, or importance, but rather the terms "first," "second," and the like are used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that elements or items preceding the word are included in the element or item listed after the word and equivalents thereof, but does not exclude other elements or items. The terms "connected" or "connected," and the like, are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", etc. are used merely to indicate relative positional relationships, which may also be changed when the absolute position of the object to be described is changed.\|[0063] For convenience of understanding, the terms involved in the embodiments of the present invention are explained below:\|[0064] Carbon sink is the process, activity or mechanism of absorbing carbon dioxide in the atmosphere by means of tree planting, vegetation recovery and the like, thereby reducing the concentration of greenhouse gases in the atmosphere. Land ecosystems such as forests, grasslands, wetlands, farmlands, deserts, cities and the like and marine ecosystems are important carbon sinks. \|[0065] Carbon sequestration and sequestration means that the carbon dioxide absorption and storage capacity of an ecosystem are increased by various means and measures, thereby reducing the concentration of carbon dioxide in the atmosphere.\|[0066] In one embodiment, as shown in fig. 1, there is provided a method for carbon sequestration and sequestration in a farmland based on silicate rock weathering, comprising the steps of:\|[0067] Step S101, obtaining agricultural management basic data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux, and carbon emission data for agricultural management. \|[0068] Specifically, agricultural management base data is acquired, the agricultural management base data including: carbon sink data based on silicate weathering, farmland environment data based on crop planting, carbon emission data based on soil carbon flux, and carbon emission data based on agricultural management. Wherein the carbon sink data based on silicate weathering comprises: silicate rock type, particle size, precipitation, application amount, weathered carbon sequestration data and the like; the farmland environment data based on crop planting includes: crop growth conditions, climate, weather, air quality, temperature and humidity and the like; carbon emission data based on soil carbon flux includes: carbon flux data, field area data, crop planting time and the like of different crop planting based on exogenous silicate rock addition; carbon emission data based on agricultural management includes: agricultural machine usage data, various kinds of agricultural machine fuel information, agricultural management measure data, and the like.\|[0069] Step S102, calculating the agricultural production management carbon emission amount according to the agricultural management basic data.\|[0070] Specifically, the estimated agricultural production management carbon emission amount can be calculated from the agricultural management base data.\|[0071] On this basis, calculating the agricultural production management carbon emission amount from the agricultural management basis data includes:\|[0072] Obtaining carbon sink quantity generated by adding exogenous silicate rock according to the silicate weathered carbon sink data and the silicate weathered carbon sink model; \|[0073] Obtaining carbon sink quantity generated by crop growth according to the farmland environment data and a carbon sink increasing model for crop planting; \|[0074] obtaining the carbon emission of the soil according to the carbon emission data of the carbon flux of the soil and a carbon emission model of the carbon flux of the soil; \|[0075] obtaining the carbon emission amount of the agricultural management according to the carbon emission data of the agricultural management and the carbon emission model of the agricultural management; \|[0076] And obtaining the agricultural production management carbon emission according to the carbon emission generated by adding the exogenous silicate rock, the carbon emission generated by growing the crops, the soil carbon emission, the agricultural management carbon emission and the farmland carbon emission prediction model of silicate rock weathering. \|[0077] Specifically, a silicate-weathered carbon sink model based on silicate-weathered silicate is built, a crop-planted carbon sequestration model based on crop planting, a soil carbon flux carbon emission model based on soil respiration and an agricultural management carbon emission model based on agricultural production management are built, a silicate-weathered farmland carbon emission prediction model is built, and the agricultural production management carbon emission amount is obtained through the silicate-weathered farmland carbon emission prediction model.\|[0078] In the embodiment, the carbon emission amount of agricultural production management is calculated by establishing a plurality of models, so that the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock-based carbon fixation and fertilizer enhancement modifier are solved, the carbon emission amount of agricultural production management can be estimated accurately, and data support is provided for ' carbon peak and ' carbon neutralization ' in the farmland field.\|[0079] On the basis, the training process of the silicate weathered carbon sink model comprises the following steps:\|[0080] Inputting silicate weathered carbon sink data serving as a network source, outputting carbon sink quantity generated by adding exogenous silicate rocks corresponding to the silicate weathered carbon sink data, applying the carbon sink data to the silicate weathered carbon sink data, and training a preset silicate weathered carbon sink model based on a random forest algorithm to obtain a silicate weathered carbon sink model; \|[0081] the carbon sink model for the weathering of the preset silicate comprises the following components: \|[0082] Wx=F(x,y,q,d)\|[0083] Wherein W x represents the carbon sink amount generated by the addition of exogenous silicate rock, F () represents a nonlinear function model, x represents a silicate type, y represents a rainfall, q represents an application amount of silicate, and d represents a silicate rock particle size. \|[0084] Specifically, a carbon sink model of pre-set silicate weathering based on a random forest algorithm is constructed, W x =f (x, y, q, d). Wherein, F () represents a nonlinear function model of silicate-decomposed carbon sequestration and silicate type, rainfall, silicate application, silicate grain size constructed by random forest algorithm. And training a carbon sink model of the preset silicate weathering through the training data set to obtain the carbon sink model of the silicate weathering which meets the expectations. And acquiring silicate rock type, particle size, precipitation, application amount and weathered carbon fixation data, and calculating the carbon dioxide fixation amount generated by silicate rock weathering, namely the carbon sink amount generated by exogenous silicate rock addition.\|[0085] On the basis, the training process of the carbon sequestration model for crop planting comprises the following steps:\|[0086] Obtaining carbon planting and sink increasing data according to the farmland environment data; \|[0087] The carbon sequestration data are input by taking the carbon sequestration data as a network source, the carbon sequestration quantity generated by the growth of crops corresponding to the carbon sequestration data is output, and the carbon sequestration data are applied to various carbon sequestration data, and training is carried out aiming at a carbon sequestration model for the preset crop planting to obtain the carbon sequestration model for the crop planting; \|[0088] wherein, the carbon sequestration model for the preset crop planting comprises: \|[0089] Zx=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi\|[0090] Wherein Z x represents the carbon sink amount generated by the growth of crops, C i represents carbon absorbed by organic substances in the synthesis unit of the whole growth period of the ith crop, Q i represents the yield of the ith crop, W i represents the moisture content of the harvest part of the ith crop, R i represents the root cap ratio of the ith crop, H i represents the economic coefficient of the ith crop, and i represents the type of the ith crop. \|[0091] Specifically, farmland environment data are obtained, and carbon planting and collection increasing data of a target area are obtained through the existing identification model. Wherein, the carbon planting and sink increasing data comprises: crop type information and plant type information, crop weight information, moisture content of harvested part of crops, root cap ratio of crops and economic coefficient of crops.\|[0092] And constructing a carbon sequestration model Z x=∑[Ci·Qi·(1-Wi)·(1+Ri)]/Hi for the preset crop planting based on the crop planting, training the carbon sequestration model for the preset crop planting through a training data set to obtain a carbon sequestration model which accords with the expected crop planting, and calculating the carbon sequestration amount generated by the crop growth according to the carbon sequestration data.\|[0093] On the basis, the training process of the carbon emission model of the soil carbon flux comprises the following steps:\|[0094] Inputting carbon emission data of the soil carbon flux as a network source, outputting the carbon emission quantity of the soil corresponding to the carbon emission data of the soil carbon flux, and training a carbon emission model of the preset soil carbon flux based on the BP neural network to obtain a carbon emission model of the soil carbon flux; \|[0095] Wherein, the carbon emission model of the preset soil carbon flux comprises: \|[0096] Fp=∑Ti·Ai,ki·ti\|[0097] Wherein F p represents the carbon emission amount of soil, T i represents the carbon flux data of the ith crop, A i represents the farmland area of the ith crop, k i represents the soil texture of the ith crop, and T i represents time. \|[0098] Specifically, a multiple regression relation between measured carbon flux data and crop planting types and soil textures is constructed, a carbon emission model of the preset soil carbon flux based on the crop types and the soil textures is determined, F p=∑Ti·Ai,ki·ti, and training of the carbon emission model of the preset soil carbon flux is carried out through a training data set, so that a carbon emission model which accords with expected soil carbon flux is obtained. And obtaining carbon flux data, field area data and crop planting time based on different crop planting of exogenous silicate rock addition, and calculating to obtain the carbon emission of the soil.\|[0099] In the embodiment, based on the BP neural network, a multiple regression relation between actually measured exogenous silicate rock added carbon flux data and crop planting types and soil textures is constructed, and the automatic calculation of the carbon emission of the soil can be realized by operating the constructed carbon emission model of the soil carbon flux.\|[0100] On this basis, the training process of the carbon emission model of agricultural management comprises the following steps:\|[0101] The carbon emission data of the agricultural management is used as a network source to be input, the carbon emission amount of the agricultural management corresponding to the carbon emission data of the agricultural management is used as an output, the carbon emission data of the agricultural management is applied to each carbon emission data of the agricultural management, and training is carried out aiming at a preset carbon emission model of the agricultural management to obtain a carbon emission model of the agricultural management; \|[0102] wherein, the carbon emission model of preset agricultural management includes: \|[0103] Mp=M1+M2+M3+M4\|[0104] M1=∑Al·Ul·αl\|[0105] M2=∑Am·Vm·αm\|[0106] M3=∑An·Wn·αn\|[0107] M4=∑Ao·αo\|[0108] Wherein M p represents an agricultural management carbon emission amount, M 1 represents an agricultural machine carbon emission amount, M 2 represents a fertilizer carbon emission amount, M 3 represents a pesticide carbon emission amount, M 4 represents a farmland cultivation and irrigation carbon emission amount, a l represents a first agricultural machine use area, U l represents a first agricultural machine use amount, a l represents a carbon emission coefficient of the first agricultural machine, l represents a first agricultural machine, a m represents an M-th chemical fertilizer use area, V m represents an M-th chemical fertilizer use amount, a m represents an M-th chemical fertilizer carbon emission coefficient, a n represents an n-th pesticide use area, W n represents an n-th pesticide use amount, a n represents an n-th pesticide carbon emission coefficient, a o represents an o-th cultivation and irrigation type use area, and a o represents an o-th cultivation and irrigation type carbon emission coefficient. \|[0109] Specifically, the use data of the agricultural machine is obtained, the agricultural management carbon emission is calculated by combining the agricultural management measure data, and the agricultural production carbon emission information is obtained. Various agricultural machine usage data include: fuel oil information of various kinds of agricultural machines, time length information of various kinds of agricultural machines, power information of various kinds of agricultural machines, and use quantity information of various kinds of agricultural machines; acquiring carbon emission factor information of various fuels based on the fuel information of various agricultural machines, and multiplying the carbon emission factor information of various fuels, the power information of various agricultural machines, the time-length information of various agricultural machines and the use quantity information of various agricultural machines to obtain the carbon emission quantity of the agricultural machines; obtaining chemical fertilizer use information and pesticide use information according to the agricultural management measure data, obtaining chemical fertilizer carbon emission factor information of various types and pesticide carbon emission factor information of various types based on the chemical fertilizer use information and the pesticide use information, calculating the product of the chemical fertilizer use information and the carbon emission factor of the corresponding chemical fertilizer type as chemical fertilizer carbon emission amount, and calculating the product of the pesticide use information and the carbon emission factor of the corresponding pesticide type as pesticide carbon emission amount; calculating the product of the cultivation and irrigation use information and the carbon emission factors of the corresponding modes as the carbon emission amount of farmland cultivation and irrigation; and combining the carbon emission of the agricultural machine, the carbon emission of the fertilizer, the carbon emission of the pesticide and the carbon emission of farmland cultivation and irrigation to obtain the carbon emission of agricultural management.\|[0110] In the embodiment, carbon emission calculation including the use of agricultural machinery, the use of chemical fertilizers and the application of pesticides in the whole agricultural management process can be realized.\|[0111] On the basis, the farmland carbon emission prediction model for silicate rock weathering comprises the following steps:\|[0112] S=Mp+Fp-Wx-Zx\|[0113] Wherein S represents an agricultural production management carbon emission amount, M p represents an agricultural management carbon emission amount, F p represents a soil carbon emission amount, W x represents an exogenous silicate rock addition carbon sink amount, and Z x represents a crop growth carbon sink amount. \|[0114] Specifically, a farmland carbon emission prediction model s=m p+Fp-Wx-Zx based on silicate rock weathering is constructed, and the agricultural production management carbon emission amount is calculated according to the model.\|[0115] Step S103, obtaining a preset farmland carbon emission target value.\|[0116] Specifically, a preset farmland carbon emission target value is set manually, and the preset farmland carbon emission target value is obtained.\|[0117] In this embodiment, a preset target carbon emission value of the farmland is set, and the optimal silicate addition amount and the optimal farmland management measure of the farmland can be determined according to the preset target carbon emission value of the farmland.\|[0118] And step S104, adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount.\|[0119] The farmland management measure adjusting method according to the preset farmland carbon emission target value and the agricultural production management carbon emission comprises the following steps:\|[0120] judging whether the agricultural production management carbon emission is larger than the preset farmland carbon emission target value; \|[0121] and adjusting farmland management measures in response to the agricultural production management carbon emission amount not being greater than the preset farmland carbon emission target value. \|[0122] Specifically, according to the agricultural production management carbon emission calculated by the silicate-weathered farmland carbon emission prediction model, judging whether the agricultural production management carbon emission is greater than a preset farmland carbon emission target value, if not, adjusting the silicate addition amount or changing the addition type and particle size and optimizing farmland management measures.\|[0123] The farmland carbon fixation and collection increasing method based on silicate rock weathering provided by the invention can calculate the carbon emission amount of agricultural production management, solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after silicate rock carbon fixation and fertilizer increase modifier is added, can accurately estimate the carbon emission amount of agricultural production management, and provides data support for ' carbon peak and ' carbon neutralization ' in the farmland field. Meanwhile, farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and a preset farmland carbon emission target value, and the aim of low carbon emission of agricultural production is achieved.\|[0124] It should be noted that, the method of the embodiment of the present invention may be performed by a single device, for example, a computer or a server. The method of the embodiment can also be applied to a distributed scene, and is completed by mutually matching a plurality of devices. In the case of such a distributed scenario, one of the devices may perform only one or more steps of the method of an embodiment of the present invention, the devices interacting with each other to accomplish the method.\|[0125] It should be noted that the foregoing describes some embodiments of the present invention. Other embodiments are within the scope of the following claims. In some cases, the actions or steps recited in the claims may be performed in a different order than in the embodiments described above and still achieve desirable results. In addition, the processes depicted in the accompanying figures do not necessarily require the particular order shown, or sequential order, to achieve desirable results. In some embodiments, multitasking and parallel processing are also possible or may be advantageous.\|[0126] Based on the same inventive concept, the invention also provides a farmland carbon fixation and exchange increasing system based on silicate rock weathering, which corresponds to the method of any embodiment.\|[0127] Referring to fig. 2, the farmland carbon sequestration and sequestration system based on silicate rock weathering includes:\|[0128] A data acquisition module 201, configured to acquire agricultural management base data; wherein the agricultural management base data includes: carbon sequestration data for silicate weathering, farmland environment data, carbon emission data for soil carbon flux and carbon emission data for agricultural management; \|[0129] An emissions calculation module 202 for calculating an agricultural production management carbon emissions based on the agricultural management base data; \|[0130] a target obtaining module 203, configured to obtain a preset target value of carbon emission in a farmland; \|[0131] and the management revision module 204 is used for adjusting farmland management measures according to the preset farmland carbon emission target value and the agricultural production management carbon emission amount. \|[0132] For convenience of description, the above system is described as being functionally divided into various modules, respectively. Of course, the functions of each module may be implemented in the same piece or pieces of software and/or hardware when implementing the present invention.\|[0133] The system of the above embodiment is used for implementing a corresponding method for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering in any of the foregoing embodiments, and has the beneficial effects of the corresponding method embodiments, which are not described herein.\|[0134] Based on the same inventive concept, the invention also provides equipment corresponding to the method in any embodiment, which comprises a memory, a processor and a computer program stored on the memory and capable of running on the processor, wherein the processor realizes the farmland carbon fixation and exchange increasing method based on silicate rock weathering in any embodiment when executing the program.\|[0135] Fig. 3 shows a more specific hardware architecture of the device provided in this embodiment, where the device may include: a processor 1010, a memory 1020, an input/output interface 1030, a communication interface 1040, and a bus 1050. Wherein processor 1010, memory 1020, input/output interface 1030, and communication interface 1040 implement communication connections therebetween within the device via a bus 1050.\|[0136] The processor 1010 may be implemented by a general-purpose CPU (Central Processing Unit ), a microprocessor, an Application SPECIFIC INTEGRATED Circuit (ASIC), or one or more integrated circuits, etc. for executing related programs to implement the technical solutions provided in the embodiments of the present disclosure.\|[0137] The Memory 1020 may be implemented in the form of ROM (Read Only Memory), RAM (Random Access Memory ), static storage, dynamic storage, etc. Memory 1020 may store an operating system and other application programs, and when the embodiments of the present specification are implemented in software or firmware, the associated program code is stored in memory 1020 and executed by processor 1010.\|[0138] The input/output interface 1030 is used to connect with an input/output module for inputting and outputting information. The input/output module may be configured as a component in a device (not shown) or may be external to the device to provide corresponding functionality. Wherein the input devices may include a keyboard, mouse, touch screen, microphone, various types of sensors, etc., and the output devices may include a display, speaker, vibrator, indicator lights, etc.\|[0139] Communication interface 1040 is used to connect communication modules (not shown) to enable communication interactions of the present device with other devices. The communication module may implement communication through a wired manner (such as USB, network cable, etc.), or may implement communication through a wireless manner (such as mobile network, WIFI, bluetooth, etc.).\|[0140] Bus 1050 includes a path for transferring information between components of the device (e.g., processor 1010, memory 1020, input/output interface 1030, and communication interface 1040).\|[0141] It should be noted that although the above-described device only shows processor 1010, memory 1020, input/output interface 1030, communication interface 1040, and bus 1050, in an implementation, the device may include other components necessary to achieve proper operation. Furthermore, it will be understood by those skilled in the art that the above-described apparatus may include only the components necessary to implement the embodiments of the present description, and not all the components shown in the drawings.\|[0142] The device of the above embodiment is used for implementing a corresponding method for carbon sequestration and sink enhancement of farmlands based on silicate rock weathering in any of the foregoing embodiments, and has the beneficial effects of the corresponding method embodiment, which are not described herein.\|[0143] Those of ordinary skill in the art will appreciate that: the discussion of any of the embodiments above is merely exemplary and is not intended to suggest that the scope of the invention (including the claims) is limited to these examples; the technical features of the above embodiments or in the different embodiments may also be combined within the idea of the invention, the steps may be implemented in any order, and there are many other variations of the different aspects of the embodiments of the invention as described above, which are not provided in detail for the sake of brevity.\|[0144] Any process or method descriptions in flow charts or otherwise described herein may be understood as representing modules, segments, or portions of code which include one or more executable instructions for implementing specific logical functions or steps of the process, and further implementations are included within the scope of the preferred embodiment of the present invention in which functions may be executed out of order from that shown or discussed, including substantially concurrently or in reverse order, depending on the functionality involved, as would be understood by those reasonably skilled in the art of the present invention.\|[0145] Where specific details are set forth in order to describe example embodiments of the invention, it should be apparent to one skilled in the art that embodiments of the invention can be practiced without, or with variation of, these specific details. Accordingly, the description is to be regarded as illustrative in nature and not as restrictive.\|[0146] While the invention has been described in conjunction with specific embodiments thereof, many alternatives, modifications, and variations of those embodiments will be apparent to those skilled in the art in light of the foregoing description.\|[0147] The present embodiments are intended to embrace all such alternatives, modifications and variances which fall within the broad scope of the appended claims. Therefore, any omissions, modifications, equivalent substitutions, improvements, and the like, which are within the spirit and principles of the embodiments of the invention, are intended to be included within the scope of the invention.	Family Number\|(110028832)\|110028832\|Object of Invention\|(CN118134720 A)\|The invention provides a method , a system and equipment for carbon fixation and sink enhancement of farmland based on silicate rock weathering , wherein the method comprises the following steps : acquiring basic agricultural management data ; wherein , the agricultural management base data includes : carbon sequestration data for silicate weathering , farmland environment data , carbon emission data for soil carbon flux and carbon emission data for agricultural management ; calculating an agricultural production management carbon emission amount according to the ( . . . ) \|The invention relates to a farmland carbon fixation and exchange increase method , system and equipment based on silicate rock weathering .\|Therefore , the invention provides a farmland carbon fixation and collection increasing method based on silicate rock weathering , which comprises the steps of firstly obtaining agriculture management basic data , then calculating the agriculture production management carbon emission according to the agriculture management basic data , and then judging whether to adjust ( . . . ) \|Abstract\|(CN118134720 A)\|The invention provides a farmland carbon sequestration and sink increase method , system and equipment based on silicate rock weathering , and the method comprises the steps : obtaining agricultural management basic data ; wherein the agricultural management basic data comprises silicate weathering carbon sink data , farmland environment data , soil carbon flux carbon emission data and agricultural management carbon emission data ; calculating agricultural production management carbon emission according to the agricultural management basic data ; acquiring a preset farmland carbon emission target value ; and adjusting farmland management measures according to a preset farmland carbon emission target value and the agricultural production management carbon emission . According to the method , the agricultural production management carbon emission can be calculated , the problem that the farmland carbon emission is unknown after the silicate rock - based carbon sequestration and fertility improvement agent is added is solved , the agricultural production management carbon emission can be accurately estimated , and data support is provided for achieving the carbon emission target . Farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and the preset farmland carbon emission target value . \|Title\|(CN118134720 A)\|Farmland carbon sequestration and sink increase method , system and equipment based on silicate rock weathering \|Advantages / Prev. Drawbacks\|(CN118134720 A)\|( . . . ) invention has the advantages that : the invention can calculate the carbon emission amount of agricultural production management , solves the problems of unclear farmland carbon fixation benefit and unclear carbon emission amount after adding the silicate rock - based carbon fixation fertilizer - increasing modifier , can accurately estimate the carbon emission amount of agricultural production management , and provides data support for carbon peak and carbon neutralization in the farmland field . \|Independent Claims\|(CN118134720 A)\|1. A farmland carbon fixation and sink enhancement method based on silicate rock weathering is characterized by comprising the following steps : Acquiring basic agricultural management data ; wherein the agricultural management base data includes : carbon sequestration data for silicate weathering , farmland environment data , carbon emission data for soil carbon flux and carbon emission data for agricultural management ; calculating an agricultural production management carbon emission amount according to the ( . . . ) \|	IT methods for management	G06N-003/08/4\|G06N-005/02/5\|G06N-005/04/1\|G06Q-010/06/3\|G06Q-050/02\|G06Q-050/26\|Y02A-090/10		G06N-003/08/4\|G06N-005/02/5\|G06N-005/04/1\|G06Q-010/06/3\|G06Q-050/02\|G06Q-050/26\|Y02A-090/10	G06N-003/084\|G06N-005/025\|G06N-005/04\|G06Q-010/063\|G06Q-050/02\|G06Q-050/26	G06N-003/084\|G06N-005/025\|G06N-005/04\|G06Q-010/063\|G06Q-050/02\|G06Q-050/26			CN120893778\|CN120450211	CN120893778 116542026 WHO=Examiner SELF=N CAT=A\|CN120450211 115573877 WHO=Examiner SELF=N CAT=A						PENDING	(CN118134720)\|PENDING	ALIVE	(CN118134720)\|ALIVE	(CN118134720)\|LEGAL DETAILS FOR CN118134720\|Actual or expected expiration date=2044-02-06\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-02-06\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202410172022\|Application date=2024-02-06\|Standardized application number=2024CN-0172022\|Event publication date=2024-06-04\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN118134720\|Publication stage code=A\|Publication date=2024-06-04\|Standardized publication number=CN118134720\|Event publication date=2024-06-04\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2024-06-21\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN118134720)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoROL0nYw6nBn1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000073002387&ekey=2254&xpn=CN118134720&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=piYDbYyO4oSmOEdPZfo6iZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN118134720)\|CN	(CN118134720)\|NAME=CHONGQING INSTITUTE OF GEOLOGY AND MINERAL RESOURCES , COUNTRY=CN		(CN118134720)\|NAME=YU HONG;CHONGQING ZHI HUI ZHI YUAN INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=50234		(CN118134720)\|NAME=MA LEI\|NAME=SI HONGTAO\|NAME=MAO ZHENG\|NAME=WANG CHEN\|NAME=LI CHENG\|NAME=XU MINGZE\|NAME=ZHU DONGXUE\|NAME=ZHU DAN\|NAME=XU WENXING	(CN118134720)\|3	1	1					(CN118134720)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2024-06-04\|Gazette number: GAZNUM=40-2301\|Number of Pages: NPAGES=15\|		(CN118134720)\|CHINESE (CHI)	(CN118134720)\|Patent	Titre: (CN118134720)\|Farmland carbon sequestration and sink increase method, system and equipment based on silicate rock weathering Résumé: (CN118134720)\|The invention provides a farmland carbon sequestration and sink increase method, system and equipment based on silicate rock weathering, and the method comprises the steps: obtaining agricultural management basic data; wherein the agricultural management basic data comprises silicate weathering carbon sink data, farmland environment data, soil carbon flux carbon emission data and agricultural management carbon emission data; calculating agricultural production management carbon emission according to the agricultural management basic data; acquiring a preset farmland carbon emission target value; and adjusting farmland management measures according to a preset farmland carbon emission target value and the agricultural production management carbon emission. According to the method, the agricultural production management carbon emission can be calculated, the problem that the farmland carbon emission is unknown after the silicate rock-based carbon sequestration and fertility improvement agent is added is solved, the agricultural production management carbon emission can be accurately estimated, and data support is provided for achieving the carbon emission target. Farmland management measures can be adjusted according to the calculated agricultural production management carbon emission and the preset farmland carbon emission target value.	0	Abstract	gpt-4o-mini	yes	The article discusses a method for carbon sequestration based on silicate rock weathering, which aligns with the topic of enhanced weathering for CO₂ capture and storage.
9	receiving an input liquid comprising at least one of seawater	brackish water	and brine effluent;																																																																			Titre: nan Résumé: nan	15		gpt-4o-mini	uncertain	No usable text found.	empty_text
10	performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream;																																																																					Titre: nan Résumé: nan	16		gpt-4o-mini	uncertain	No usable text found.	empty_text
11	CN202210271537	CN202310250007\|CN202210271537	CN116463001\|CN116463001\|CN114574045	100341084	CN116463001 B 2024-07-05 [CN116463001B]\|CN116463001 A 2023-07-21 [CN116463001]\|CN114574045 A 2022-06-03 [CN114574045]	2022-03-18	2023-03-15\|2022-03-18	2024-07-05\|2023-07-21\|2022-06-03	(CN116463001B)\|2024-07-05\|	(CN116463001)\|2043-03-15\|(CN114574045)\|2023-08-29	(CN116463001)\|Water medium carbon dioxide capturing surface layer coating and preparation method thereof	(CN116463001)\|The invention discloses a water medium carbon dioxide capture surface coating and a preparation method thereof. The water medium carbon dioxide capture surface coating is formed by mixing polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, kieselguhr, calcium silicate, rock wool fibers and thin cement paste according to a certain mass ratio. The mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the coating is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; and the mass ratio of the thin cement paste in the coating is 35-57%. The coating is smeared on the surface of a building, and when a coating layer is dry, carbon dioxide can be automatically captured from air; when the coating layer is wet, the coating layer can desorb carbon dioxide and dissolve the carbon dioxide in water in a carbonate form to flow out, so that the carbon breathing function of the external facade of the building is realized.	DONGHUA UNIVERSITY\|SHANGHAI ZEYAO ENV PROT TECHNOLOGY	(CN116463001)\|SHANGHAI ZEYAO ENV PROT TECH CO LTD ([CN])\|DONGHUA UNIVERSITY\|(CN116463001)\|SHANGHAI ZEYAO ENV PROT TECH CO LTD ([CN])\|DONGHUA UNIVERSITY\|(CN114574045)\|SHANGHAI ZEYAO ENV PROT TECH CO LTD ([CN])\|DONGHUA UNIVERSITY	SONG XINSHAN\|XU YONG\|ZHANG ZHILAN\|WANG YUHUI\|XU ZHONGSHUO\|WANG YIFEI\|LIU YINGYING\|TAN SHUJUAN\|HUANG NA\|TANG HAIYAN	(CN116463001)\|Song Xinshan\|Xu Yong\|Zhang Zhilan\|Wang Yuhui\|Xu Zhongshuo\|Wang Yifei\|Liu Yingying\|Tan Shujuan\|Huang Na\|Tang Haiyan\|(CN116463001)\|SONG XINSHAN\|XU YONG\|ZHANG ZHILAN\|WANG YUHUI\|XU ZHONGSHUO\|WANG YIFEI\|LIU YINGYING\|TAN SHUJUAN\|HUANG NA\|TANG HAIYAN	(CN116463001)\|XU HAOJUN;SHANGHAI JIANQIU INTELLECTUAL PROPERTY ATTORNEYS\|Reg. Nb: 31382\|(CN114574045)\|HE XINXIN;Hefei Du Lei Intellectual Property Agency (General Partnership)\|Reg. Nb: 34227	(CN116463001)\|In practice, however, there are a number of substances that can achieve carbon dioxide adsorption, but it is difficult to achieve regeneration under normal environmental conditions (condition (4) is not satisfied), because they must overcome a large energy barrier to regenerate.\|	(CN116463001)\|1. The preparation method of the water medium carbon dioxide capturing surface layer coating is characterized by comprising polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion; Wherein the mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%; the hydrotalcite-like mineral is layered double metal hydroxide formed by Ca/Al/Mg metal oxide, is from natural hydrohead mineral, is assembled by positively charged octahedral main body laminates and interlayer anions through non-covalent bond interaction, and has the particle size range of 0.1-1.0mm; the paint is applied to the surface of a building, carbon dioxide can be automatically captured from the air when the paint layer is dry, and the paint layer can desorb the carbon dioxide and dissolve in water in the form of carbonate to flow out when the paint layer is wet. \|	(CN116463001)\|The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried; when the air is wet, carbon dioxide in the gaps of the coating layer is converted into carbonate or bicarbonate to be released, and the carbonate or bicarbonate is flushed with water to enter the water body, so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled, and the problems in the background art are solved. In order to achieve the above purpose, the present invention provides the following technical solutions:\|The invention discloses a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the coating is composed of polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion; the mass ratio of the polystyrene quaternary ammonium salt resin in the paint is 10-15%; the mass ratio of hydrotalcite-like minerals in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the paint is 17-25%; the mass ratio of the rock wool fiber in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%.\|The invention relates to the technical field of carbon capture, in particular to a water-medium carbon dioxide capture surface layer coating and a preparation method thereof.\|	(CN116463001)\|CARBON DIOXIDE(100,61)\|HYDROTALCITE MINERAL(100,25)\|COATING LAYER(100,19)\|WATER MEDIUM(100,8)\|WATER MEDIUM CARBON DIOXIDE(100,8)\|MEDIUM CARBON DIOXIDE(100,2)\|SURFACE LAYER COATING(100,2)\|QUATERNARY AMMONIUM SALT RESIN(80,22)\|ROCK WOOL FIBER(79,11)\|NATURAL HYDROHEAD MINERAL(66,1)\|AMMONIUM SALT RESIN(62,22)\|PAINT LAYER(62,6)\|PAINT(55,17)\|CEMENT SLURRY(53,10)\|NONCOVALENT BOND INTERACTION(49,3)\|WOOL FIBER(47,14)\|SALT RESIN(46,22)\|POLYSTYRENE(42,28)\|INTERLAYER ANION(41,3)\|DIATOMITE(38,16)\|OCTAHEDRAL MAIN BODY LAMINATE(36,1)\|DIATOMITE MASS RATIO(35,3)\|CALCIUM SILICATE(34,23)\|BICARBONATE(32,2)\|MASS RATIO(30,29)\|CARBON DIOXIDE CAPTURE(30,4)\|HYDROTALCITE MINERAL MASS RATIO(30,2)\|BONDING INTERACTION(28,3)\|LAMINATING BODY(28,1)\|CARBON DIOXIDE ADSORPTION(26,1)\|REGENERATION(24,1)\|SPRAY FUNCTIONAL COATING(24,1)\|COATING LAYER GAP(23,1)\|LAYERED DOUBLE METAL HYDROXIDE(20,3)\|WATERBORNE(18,1)\|CALCIUM SILICATE PARTICLE(17,4)\|LAYERED DOUBLE METAL(17,3)\|WATER CARBON DIOXIDE(16,3)\|CARBON CAPTURE(13,1)\|STRUCTURE OUTER FACADE(12,1)\|CAPTURING SURFACE LAYER(11,4)\|CARBON RESPIRATION(11,2)\|DIATOMITE PARTICLE(10,3)\|INTENSIVE QUATERNIZATION(10,2)\|PARTICLE SIZE(9,16)\|DIRECTLY SMEARED COATING(9,3)\|MG METAL OXIDE(9,3)\|POWDER SHAPE(9,3)\|ENVIRONMENTAL CONDITION(9,2)\|LARGE ENERGY BARRIER(9,1)\|AMMONIUM SALT(8,8)\|CHLORO METHYL POLYSTYRENE(8,2)\|WATER BODY(8,2)\|HYDROTALCITE MINERAL PARTICLE(8,1)\|MAGNESIA OCTAHEDRON(8,1)\|NATURAL HYDROHEAD ORE(8,1)\|OCTAHEDRAL HOST LAMINATE(8,1)\|CA AL(7,3)\|BUILDING OUTER FACADE(7,2)\|POLYSTYRENE RESIN POWDER PARTICLE(7,2)\|COATING MILDEW PREVENTION(7,1)\|INFRARED GAS ANALYZER LICOR(7,1)\|JINING SANSHI BIOTECHNOLOGY CO(7,1)\|NATURAL HYDROTALCITE MINERAL(7,1)\|OBSERVATION INSTRUMENT(7,1)\|ALUMINA OCTAHEDRON(6,1)\|AMINE ADSORBENT(6,1)\|PREPARED SURFACE COATING(6,1)\|TECHNICAL FEATURE(5,3)\|ALUMINUM MAGNESIUM HYDROTALCITE(5,2)\|FLAME RETARDANCE FUNCTION(5,2)\|POLYETHYLENIMINE(5,2)\|QUATERNARY AMMONIUM ION EXCHANGE(5,2)\|NATURAL HYDROFLUORITE(5,1)\|SOAKING(4,4)\|ANTIBIOSIS(4,2)\|BROMOBUTANE(4,2)\|BROMODODECANE(4,2)\|CARBON DIOXIDE ABSORPTION(4,2)\|ISOPROPANOL(4,2)\|PRESERVATION(4,2)\|SAMPLE CELL(4,2)\|SAMPLE CHAMBER(4,2)\|ALUMINUM CALCIUM HYDROTALCITE(4,1)\|BICARBONATE FORMATION(4,1)\|CONTRADICTION(4,1)\|DISPERSING MACHINE(4,1)\|DRIED TILE(4,1)\|HYDROTALCITE MINERAL SCHEMATIC DIAGRAM(4,1)\|INORGANIC PARTICLE(4,1)\|MASS SHARE(4,1)\|MILDEW PROOF(4,1)\|MILDEW RESISTANCE(4,1)\|PREMIXING(4,1)\|RAPID REGENERATION(4,1)\|WATER VAPOR COMPETITIVE ADSORPTION(4,1)\|HCO(3,3)\|ADSORPTION DESORPTION(3,1)\|BEAKER(3,1)\|BICARBONATE ANION(3,1)\|\|(CN116463001)\|CARBON DIOXIDE(100,64)\|HYDROTALCITE MINERAL(100,26)\|COATING LAYER(100,20)\|WATER MEDIUM(100,9)\|WATER MEDIUM CARBON DIOXIDE(100,9)\|MEDIUM CARBON DIOXIDE(100,2)\|SURFACE LAYER COATING(100,2)\|QUATERNARY AMMONIUM SALT RESIN(96,25)\|ROCK WOOL FIBER(90,12)\|AMMONIUM SALT RESIN(75,25)\|PAINT(57,18)\|CEMENT SLURRY(56,10)\|SALT RESIN(55,25)\|WOOL FIBER(54,15)\|POLYSTYRENE(50,30)\|DIATOMITE(42,17)\|DIATOMITE MASS RATIO(42,4)\|CALCIUM SILICATE(40,25)\|NATURAL HYDROTALC ORE(39,1)\|MASS RATIO(36,36)\|OCTAHEDRAL HOST LAMINATE(36,2)\|NONCOVALENT INTERACTION(34,1)\|PAINT LAYER(32,3)\|INTENSIVE QUATERNIZATION(29,3)\|WATERBORNE CARBON DIOXIDE(29,2)\|HYDROTALCITE MINERAL MASS RATIO(28,2)\|CARBON DIOXIDE CAPTURE(27,5)\|BICARBONATE(27,3)\|INTERLAYER ANION(25,3)\|CHLORO METHYL POLYSTYRENE(24,3)\|CARBON DIOXIDE ADSORPTION(24,1)\|REGENERATION(22,1)\|POLYSTYRENE RESIN POWDER PARTICLE(21,3)\|COATING LAYER GAP(21,1)\|WATER CARBON DIOXIDE(17,4)\|CALCIUM SILICATE PARTICLE(16,4)\|POLYETHYLENIMINE(16,3)\|SOAKING(14,6)\|BROMODODECANE(14,3)\|BROMOBUTANE(13,3)\|CAPTURING SURFACE LAYER(12,5)\|ISOPROPANOL(12,3)\|LAYERED DOUBLE METAL HYDROXIDE(12,3)\|CARBON CAPTURE(12,1)\|CARBON RESPIRATION(11,2)\|STRUCTURE OUTER FACADE(11,1)\|DIATOMITE PARTICLE(10,3)\|SWELLING(10,3)\|POWDER SHAPE(9,3)\|ENVIRONMENTAL CONDITION(9,2)\|NONCOVALENT BOND INTERACTION(9,2)\|WATER BODY(8,2)\|LARGE ENERGY BARRIER(8,1)\|PARTICLE SIZE(7,16)\|BUILDING OUTER FACADE(7,2)\|HYDROTALCITE MINERAL PARTICLE(7,1)\|MAGNESIA OCTAHEDRON(7,1)\|NATURAL HYDROHEAD ORE(7,1)\|COATING MILDEW PREVENTION(6,1)\|INFRARED GAS ANALYZER LICOR(6,1)\|JINING SANSHI BIOTECHNOLOGY CO(6,1)\|NATURAL HYDROTALCITE MINERAL(6,1)\|OBSERVATION INSTRUMENT(6,1)\|MG METAL OXIDE(5,3)\|TECHNICAL FEATURE(5,3)\|ALUMINUM MAGNESIUM HYDROTALCITE(5,2)\|BONDING INTERACTION(5,2)\|FLAME RETARDANCE FUNCTION(5,2)\|ALUMINA OCTAHEDRON(5,1)\|PREPARED SURFACE COATING(5,1)\|CA AL(4,3)\|ROOM TEMPERATURE(4,3)\|ANTIBIOSIS(4,2)\|CARBON DIOXIDE ABSORPTION(4,2)\|PRESERVATION(4,2)\|SAMPLE CELL(4,2)\|SAMPLE CHAMBER(4,2)\|NATURAL HYDROFLUORITE(4,1)\|ALUMINUM CALCIUM HYDROTALCITE(3,1)\|BICARBONATE FORMATION(3,1)\|CLOSED PLEXIGLASS(3,1)\|CONTRADICTION(3,1)\|DISPERSING MACHINE(3,1)\|DRIED TILE(3,1)\|HYDROTALCITE MINERAL SCHEMATIC DIAGRAM(3,1)\|INORGANIC PARTICLE(3,1)\|MASS SHARE(3,1)\|MILDEW PROOF(3,1)\|MILDEW RESISTANCE(3,1)\|POLYSTYRENETHE CARBON DIOXIDE(3,1)\|PREMIXING(3,1)\|RAPID REGENERATION(3,1)\|\|(CN114574045)\|CARBON DIOXIDE(100,64)\|WATERBORNE CARBON DIOXIDE(100,15)\|COATING SURFACE(100,6)\|HYDROTALCITE MINERAL(97,21)\|ROCK WOOL FIBER(82,18)\|QUATERNARY AMMONIUM SALT RESIN(77,22)\|CCS ALONE2THE STABILITY(72,1)\|CEMENT SLURRY(70,8)\|AMMONIUM SALT RESIN(60,22)\|WOOL FIBER(51,8)\|CARBON DIOXIDE CAPTURE TOPCOAT(49,3)\|DIATOMITE(47,16)\|COATING LAYER(47,15)\|AUTOMATIC CAPTURE(46,3)\|SALT RESIN(44,22)\|POLYSTYRENE(41,29)\|NONCOVALENT BOND INTERACTION(37,3)\|CALCIUM SILICATE(31,19)\|DIATOMITE PARTICLE(29,4)\|INTERLAYER ANION(29,3)\|WATERBORNE CARBON DIOXIDE CAPTURE(27,2)\|REGENERATION(26,1)\|ENHANCED QUATERNIZATION(25,3)\|POLYSTYRENE RESIN POWDER PARTICLE(25,3)\|BICARBONATE(25,1)\|COATING LAYER GAP(25,1)\|DIFFICULT TASK(25,1)\|OCTAHEDRAL MAIN(25,1)\|NATURAL HYDROTALCITE(24,4)\|CARBON DIOXIDE AUTOMATIC CAPTURE(23,2)\|OUTER FACADE(23,2)\|CARBON DIOXIDE ADSORPTION(22,2)\|FOSSIL FUEL(21,1)\|GLOBAL WARMING PREVENTION(21,1)\|SPRAYING(19,4)\|ENERGY INFRASTRUCTURE(19,1)\|CALCIUM SILICATE PARTICLE(18,4)\|POLYETHYLENEIMINE(18,3)\|ANTIFUNGAL FUNCTION(17,1)\|SOAKING(16,7)\|MIXING RATIO MASS(16,5)\|ANTIBACTERIAL(16,2)\|WATER MEDIUM(16,1)\|COATING FUNCTION(15,3)\|PRESERVATION(15,3)\|FLAME RETARDANT(14,2)\|CARBON CAPTURE(14,1)\|MASS RATIO(13,18)\|ISOPROPANOL(13,3)\|STRUCTURE OUTER FACADE(13,2)\|COATING VOID RATIO(11,3)\|SWELLING(11,3)\|MIXING RATIO(10,5)\|POWDER SHAPE(10,3)\|ENVIRONMENTAL CONDITION(10,2)\|LARGE ENERGY BARRIER(10,1)\|WATER BODY(9,2)\|CO2AMINE SORBENT(9,1)\|HYDROTALCITE MINERAL PARTICLE(9,1)\|DIRECTLY COATED COATING(8,3)\|COATING MILDEW PREVENTION(8,1)\|COMPETITIVE ADSORPTION(8,1)\|INFRARED GAS ANALYZER LICOR(8,1)\|OBSERVATION INSTRUMENT(8,1)\|RENEWABLE ENERGY SOURCE(8,1)\|MASS FRACTION(7,3)\|HEAT INSULATION(7,2)\|SAMPLE CHAMBER(6,4)\|AQUEOUS MEDIUM(6,2)\|BONDING INTERACTION(6,2)\|BUILDING OUTER VERTICAL SURFACE(6,1)\|CREATIVE EFFORT(6,1)\|MILDEW PROOF(6,1)\|OCTAHEDRAL HOST(6,1)\|TRANSITION PERIOD2CAPTURE(6,1)\|CA AL(5,3)\|GAS EXCHANGE(5,3)\|MG METAL OXIDE(5,3)\|BICARBONATE RADICAL FORMATION(5,1)\|LAYERED DOUBLE HYDROXIDE(5,1)\|OUTER VERTICAL SURFACE(5,1)\|RAPID REGENERATION(5,1)\|SURFACE LAYER(5,1)\|HCO(4,4)\|ROOM TEMPERATURE(4,3)\|TILE(4,3)\|AIR2ABSORPTION(4,1)\|CAPTURE RELEASE CIRCULATION(4,1)\|CLOSED PLEXIGLASS CHAMBER(4,1)\|CO2A CAPTURE RELEASE CYCLE(4,1)\|DISPERSION MACHINE(4,1)\|FLAME RETARDANCE FUNCTION(4,1)\|HANDTHE(4,1)\|INORGANIC PARTICLE(4,1)\|MOISTURE BOUND(4,1)\|PARTICLE SIZE RANGE(4,1)\|	(CN116463001)\|1. The preparation method of the water medium carbon dioxide capturing surface layer coating is characterized by comprising polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion;\| Wherein the mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%; \| the hydrotalcite-like mineral is layered double metal hydroxide formed by Ca/Al/Mg metal oxide, is from natural hydrohead mineral, is assembled by positively charged octahedral main body laminates and interlayer anions through non-covalent bond interaction, and has the particle size range of 0.1-1.0mm; \| the paint is applied to the surface of a building, carbon dioxide can be automatically captured from the air when the paint layer is dry, and the paint layer can desorb the carbon dioxide and dissolve in water in the form of carbonate to flow out when the paint layer is wet. \|2. The method for preparing the water-based carbon dioxide capturing surface layer paint according to claim 1, wherein the polystyrene quaternary ammonium salt resin adopts commercial powder particles with the particle size of 0.2-1.0mm.\|3. The method for preparing the water-based carbon dioxide capturing surface layer paint according to claim 1, wherein the diatomite is in a powder shape and has a particle size of 0.5-1.0mm.\|4. The method for preparing the water-borne carbon dioxide capturing surface layer coating according to claim 1, wherein the particle size of the calcium silicate particles is in the range of 0.1-0.5mm and the relative density is 2.5-3.0.\|5. The method for preparing the water-based carbon dioxide capture surface coating according to claim 1, wherein the rock wool fibers are common rock wool fibers.\|6. The method for preparing the water-based carbon dioxide capturing surface layer paint as claimed in claim 1, comprising:\| Mixing dilute cement paste with the water cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers according to a certain mass ratio, and uniformly stirring to obtain a directly-smeared coating; or (b) \|The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray-type functional coating is obtained.\|7. The method for preparing the water-based carbon dioxide capture surface coating according to claim 1, wherein the prepared surface coating can be directly smeared or sprayed on the outer surface of a structure, and the thickness of the coating is 0.2-0.5cm.	(CN116463001)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of carbon capture, in particular to a water-medium carbon dioxide capture surface layer coating and a preparation method thereof.\|BACKGROUND ART\|[0002] The capture and sequestration (CCS) of high concentration CO 2 emitted by point sources during the transition period may reduce the emissions of CO 2. However, the aim of stabilizing the CO 2 in the atmosphere below 450ppm is not possible with CCS alone. The concentration of carbon dioxide in air has increased from around 200ppm before the industrial revolution to over 400ppm at present, and therefore, the development of technology for directly capturing carbon dioxide from the surrounding air is also an effective means for slowing down climate change and is urgent.\|DISCLOSURE\|Disclosure of Invention\|[0003] The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried; when the air is wet, carbon dioxide in the gaps of the coating layer is converted into carbonate or bicarbonate to be released, and the carbonate or bicarbonate is flushed with water to enter the water body, so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled, and the problems in the background art are solved.\|[0004] In order to achieve the above purpose, the present invention provides the following technical solutions:\|[0005] A preparation method of water medium carbon dioxide capturing surface layer coating comprises polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion; wherein the mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%. \|[0006] Furthermore, the polystyrene quaternary ammonium salt resin is a main component for capturing carbon dioxide in a water medium, and can be prepared by adopting commercial powder particles or self-preparation, and the particle size is 0.2-1.0mm.\|[0007] Further, the preparation method of the polystyrene quaternary ammonium salt resin comprises the following steps:\|[0008] s1: completely immersing 10 parts of chloromethyl polystyrene resin powder in N, N-Dimethylformamide (DMF) according to the mass ratio, and swelling for 24 hours at 30-40 ℃; \|[0009] s2: adding 2 parts of polyethylenimine, and soaking for 12 hours at 30-40 ℃; \|[0010] s3: soaking in ethanol for 12 hours, filtering and drying; \|[0011] S4: swelling with isopropanol for 24 hours, adding 5 parts of 1 bromododecane for quaternization at 80-85 ℃ for 24 hours, and then adding 1.5 parts of 1 bromobutane for intensive quaternization at 45-50 ℃ for 4 hours; \|[0012] s5: and finally, filtering at room temperature, washing with ethanol and drying to obtain the quaternary ammonium salt modified polystyrene resin powder particles. \|[0013] Further, the hydrotalcite-like mineral is a layered double metal hydroxide composed of Ca/Al/Mg metal oxide, which is derived from natural hydrohead ore, and is assembled by non-covalent bond interaction between positively charged octahedral host laminates and interlayer anions, and has a particle size ranging from 0.1 to 1.0mm.\|[0014] Furthermore, the diatomite is in a powder shape, the particle size is 0.5-1.0mm, and the huge specific surface area of the diatomite particles is beneficial to the adsorption and exchange of gas.\|[0015] Furthermore, the particle size range of the calcium silicate particles is 0.1-0.5mm, and the relative density is 2.5-3.0, so that the calcium silicate has the functions of flame retardance, heat preservation, heat insulation, antibiosis and mildew prevention.\|[0016] Furthermore, the rock wool fiber is common rock wool fiber and is used for increasing the void ratio of the coating and facilitating gas exchange.\|[0017] Still further, the method includes:\|[0018] Mixing dilute cement paste with the water cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers according to a certain mass ratio, and uniformly stirring to obtain a directly-smeared coating; or (b) \|[0019] The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray coating type paint is obtained.\|[0020] Furthermore, the prepared surface layer coating can be directly and uniformly coated or sprayed on the outer surface of the structure, the thickness of the coating is 0.2-0.5cm, and the carbon respiration function of the outer surface of the structure can be realized, namely, carbon dioxide is absorbed when air is gradually dried, and carbon dioxide is released when the air is wet.\|[0021] Compared with the prior art, the invention has the beneficial effects that:\|[0022] The invention provides a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the water medium carbon dioxide capturing surface layer coating is mainly composed of polystyrene quaternary ammonium salt resin (mass portion 10-15), hydrotalcite-like minerals (mass portion 10-15), diatomite (mass portion 3-5), calcium silicate (mass portion 17-25), rock wool fibers (mass portion 3-5) and dilute cement paste (mass portion 35-57) according to a certain mass mixing proportion, the coating is smeared on the surface of a building, carbon dioxide can be automatically captured from air when a coating layer is dried, carbon dioxide can be desorbed by the coating layer and dissolved in water in a carbonate form to flow out when the coating layer is wet, the carbon dioxide in the air is automatically captured by taking water as a medium, and the carbon dioxide breathing function of the outer facade of the building can be realized. \|[0023] The conception, specific structure, and technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, features, and effects of the present invention.\|DRAWINGS DESCRIPTION\|[0024] The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate embodiments of the application and together with the description serve to explain the application.\|[0025] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for the description of the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0026] FIG. 1 is a schematic illustration of the carbon dioxide absorption and release process mechanism of the coating of the present invention;\|[0027] FIG. 2 is a schematic illustration of the application of the coating of the present invention to a facade of a structure; \|[0028] FIG. 3 is a schematic diagram of hydrotalcite-like minerals according to the present invention. \|INVENTION MODE\|Detailed Description\|[0029] Other advantages and effects of the present invention will become apparent to those skilled in the art from the following disclosure, which describes the embodiments of the present invention with reference to specific examples. The invention may be practiced or carried out in other embodiments that depart from the specific details, and the details of the present description may be modified or varied from the spirit and scope of the present invention. It should be noted that the following embodiments and features in the embodiments may be combined with each other without conflict.\|[0030] It should be noted that the illustrations provided in the following embodiments merely illustrate the basic concept of the present invention by way of illustration, and only the components related to the present invention are shown in the illustrations, not according to the number, shape and size of the components in actual implementation, and the form, number and proportion of each component in actual implementation may be arbitrarily changed, and the layout of the components may be more complex.\|[0031] Some exemplary embodiments of the invention have been described for illustrative purposes, it being understood that the invention may be practiced otherwise than as specifically shown in the accompanying drawings.\|[0032] The embodiment of the invention provides a preparation method of a water medium carbon dioxide capturing surface layer coating, which consists of polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion.\|[0033] The polystyrene quaternary ammonium salt resin is a main component for realizing carbon dioxide capture of a water medium, can be prepared from commercial powder particles with the particle size of 0.2-1.0mm, has the mass ratio of 10-15% in the coating, and has a certain mildew-proof and bactericidal effect and is beneficial to mildew prevention of the coating.\|[0034] The preparation method of the polystyrene quaternary ammonium salt resin comprises the following steps:\|[0035] s1: completely immersing 10 parts of chloromethyl polystyrene resin powder in N, N-Dimethylformamide (DMF) according to the mass ratio, and swelling for 24 hours at 30-40 ℃; \|[0036] s2: adding 2 parts of polyethylenimine, and soaking for 12 hours at 30-40 ℃; \|[0037] s3: soaking in ethanol for 12 hours, filtering and drying; \|[0038] S4: swelling with isopropanol for 24 hours, adding 5 parts of 1 bromododecane for quaternization at 80-85 ℃ for 24 hours, and then adding 1.5 parts of 1 bromobutane for intensive quaternization at 45-50 ℃ for 4 hours; \|[0039] s5: and finally, filtering at room temperature, washing with ethanol and drying to obtain the quaternary ammonium salt modified polystyrene resin powder particles. \|[0040] The synthetic process route of the polystyrene quaternary ammonium salt resin is as follows:\|[0041] \|[0042] In the embodiment of the invention, the hydrotalcite-like mineral is mainly a layered double metal hydroxide formed by Ca/Al/Mg metal oxide, is derived from natural hydrofluorite, is assembled by non-covalent bond interaction between a main body laminate of an octahedron (calcoxy, magnesia octahedron or alumina octahedron) with positive charges and an interlayer anion, and has a structure shown in figure 3 (wherein M represents Ca, al or Mg; A represents an anion). \|[0043] In order to reduce cost, natural hydrotalcite-like minerals can be directly adopted, the particle size range of the hydrotalcite-like minerals is 0.1-1.0mm, and the mass ratio of the hydrotalcite-like minerals in the paint is 10-15%.\|[0044] Specifically, hydrotalcite-like minerals can be purchased from the following web sites:\|[0045] aluminum magnesium hydrotalcite (Tianjin balance blue sea technology limited): \|[0046] https://detail.1688.com/offer/661622986146.htmlexp=enquiry%3AB&spm=a312h.2018_new_sem.dh_002.4.753e4b3dwFlIOj&cosite=baidujj&tracelog=p4p&_p_isad=1&clickid=d03616eec8864d809dce520d1839c01d&sessionid=cfdd5b610ea8464e0d77c3b1871a9264&a=1416&e=KWo.0gR-IlmQgV3XCjgNJ7LfaupOvlS.jc7eTz15fCH9PqbBDDQSDzB3m4XMOgA2e2OtVP1Jh4sb7AJCzkOHH5ZgSgUQMMbOH9p4ldzbdqEkTW.VtH..9uIaYQ4Zs.dt.o8k8junxwtz3zM49yD9eKsE2ZV6JcpvnCOJLKxPYQ96Hg0R6Cv1gtCPyb20.DQ8nuhLQNZ9dqHjqfl.RGtZYkVHyVZEqONRqtYzmCIrysY3GBxjBoOQaM5Jy6mnZopXvloJuMZHzzi885SgK3ZLXw__&sk=sem&style=1.\|[0047] aluminum magnesium hydrotalcite (Jin Shuiou Hongyuan chemical industry business, zheng state): \|[0048] https://detail.1688.com/offer/588588278288.html&idx=50。\|[0049] Aluminum-calcium hydrotalcite (Jining Sanshi biotechnology Co., ltd.): \|[0050] https://detail.1688.com/offer/677407307296.html&idx=55。\|[0051] The hydrotalcite-like mineral is helpful for the paint to realize the adsorption and release of carbonate anions and bicarbonate anions. Meanwhile, the hydrotalcite mineral has the capability of absorbing infrared light with specific wavelength, can accelerate the heating and drying of the paint, accelerates the absorption of carbon dioxide by the paint, and is more conducive to the realization of the absorption of infrared wave bands after the hydrotalcite-like mineral is combined with the organic ion exchange resin. \|[0052] The diatomite in the embodiment of the invention is in a powder shape, the particle size is 0.5-1.0mm, the mass fraction is 3-5%, and the huge specific surface area of the diatomite particles is beneficial to the adsorption and exchange of gas.\|[0053] The particle size range of the calcium silicate particles in the embodiment of the invention is 0.1-0.5mm, the relative density is 2.5-3.0, the mass ratio of the calcium silicate particles in the coating is 17-25%, and the calcium silicate can increase the functions of flame retardance, heat preservation, heat insulation, antibiosis and mildew resistance of the surface of a structure.\|[0054] The rock wool fiber in the embodiment of the invention is common basalt rock wool fiber, the mass share of the rock wool fiber is 3-5%, the fiber length is 1-5cm, and the rock wool fiber has the main function of increasing the void ratio of the coating and is beneficial to gas exchange.\|[0055] According to the application mode of the coating, the water-cement ratio of the dilute cement slurry is divided into two types, and the dilute cement slurry with the water-cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly stirred according to a certain mass ratio, so that the directly smeared coating is obtained; or alternatively\|[0056] The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray coating type paint is obtained.\|[0057] The carbon breath of the structure to carbon dioxide can be realized by painting the paint on the outer surface of the structure (the thickness of the coating is 0.2-0.5 cm), namely, carbon dioxide is absorbed when air is gradually dried, and carbon dioxide is released when the air is wet.\|[0058] The research and development principle of the invention: according to prior art documents, materials that successfully achieve direct capture of carbon dioxide from air generally require that 4 conditions be met:\|[0059] (1) Rapid reaction kinetics, and can rapidly absorb carbon dioxide; (2) the cost is low enough to facilitate the development and popularization of the application; (3) the application scene is wide, and large-scale application can be developed; (4) The method is convenient for rapid regeneration under general environmental conditions, and can complete the whole CO 2 capturing-releasing cycle. \|[0060] In practice, however, there are a number of substances that can achieve carbon dioxide adsorption, but it is difficult to achieve regeneration under normal environmental conditions (condition (4) is not satisfied), because they must overcome a large energy barrier to regenerate. For example, the heat of adsorption required for the calcium-based calcination process and the sodium-based decomposition hydrolysis process are 179kJ/mol CO 2 and 135kJ/mol CO 2, respectively, and the amine-based adsorbent has a heat of adsorption for CO 2 of about 80kJ/mol CO 2, respectively. They require a large amount of energy if they need to be released again after adsorbing carbon dioxide, which in turn leads to carbon dioxide emissions.\|[0061] Therefore, the embodiment of the invention provides the energy-saving adsorbent taking water as a medium, carbon dioxide can be captured and released only by means of the water medium in contact with the material, compared with other adsorption materials, the adsorption heat of the ion exchange resin is only 32kJ/mol CO 2, and when the relative humidity of air is increased from 15% to 100%, the equilibrium partial pressure of CO 2 on the polystyrene quaternary ammonium salt ion exchange resin is increased by 2 orders of magnitude, namely, the carbon dioxide adsorbed in the polystyrene quaternary ammonium salt ion exchange resin is obviously released due to the increase of the air humidity. This effect is due on the one hand to the physical competitive adsorption of water vapor and carbon dioxide by the polystyrene quaternary ammonium ion exchange resin and on the other hand to the good affinity of the polystyrene quaternary ammonium ion exchange resin for CO 2 when dried.\|[0062] The principle of the polystyrene quaternary ammonium salt ion exchange resin is as follows: with the air-drying process in-line with the air-drying process, The positively charged adsorbed CO 32- in the quaternary ammonium salt and water molecules in the material gaps are converted into HCO 3-, Thereby freeing up an adsorption site for the absorption of OH -, while OH - absorbs CO 2 from the air and converts it to HCO 3-, the process thus achieves direct capture of carbon dioxide in the air; when the air is wet, the air is in contact with the air, The 2 HCO 3- are combined and converted into CO 32- and CO 2 are carried away by water, Part of CO 32- occupies 2 positive charge adsorption sites in the quaternary ammonium salt. I.e., adsorption/desorption of CO 2, can be expressed as a series of reactions: dissociation of water, formation of bicarbonate, adsorption of CO 2 on hydroxide, release of carbonate from bicarbonate back and release of CO 2. The main chemical process is shown in the following formula and is shown in the attached figure 1.\|[0063] H2O=H++OH-\|[0064] CO32-+H+=HCO3-\|[0065] OH-+CO2=HCO3-\|[0066] HCO3-+HCO3-=CO32-+CO2+H2O\|[0067] In order to meet 4 conditions of successfully realizing direct capture of carbon dioxide materials from air, the embodiment of the invention provides a water medium carbon dioxide capture surface layer coating and a preparation method thereof. Mainly comprises polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion.\|[0068] For further better explanation of the invention, the following specific embodiments are provided:\|[0069] 10 g of polystyrene quaternary ammonium salt ion exchange resin balls (particle size of 0.5 mm), 10 g of hydrotalcite mineral particles (particle size of 0.5 mm), 3 g of diatomite particles (particle size of 0.5-1.0 mm), 17 g of calcium silicate (particle size of 0.5 mm), 3 g of rock wool fibers (basalt fibers for common insulation boards) and 57 g of dilute cement paste (water cement ratio of 0.75) are mixed, firstly, manual pre-mixing is carried out, then the mixture is put into a beaker, and mechanical mixing is carried out for 30min by using a dispersing machine, and the stirring speed is 18-22r/min. About 100 grams of coating was finally obtained. \|[0070] As shown in FIG. 2, a portion of the coating was spread on a 10cm by 10cm tile surface to a thickness of 0.5mm and then dried in a vacuum oven at 105℃for 24 hours to ensure complete drying of the coating, which removed carbon dioxide and moisture incorporated within the coating. The tile is then quickly placed in a sample cell (30 cm x 30cm closed plexiglass box) that is connected to an infrared gas analyzer LICOR840, and the carbon dioxide concentration and dew point (the greater the relative humidity, the higher the dew point temperature) of the sample cell can be obtained in real time.\|[0071] As can be seen by instrumental observation, the concentration of carbon dioxide in the sample chamber was reduced from 800ppm to 400ppm over 60min and to 320ppm over 120min after the dried tile coated with the coating was placed, indicating that the dried coating layer had the ability to absorb ("call in") carbon dioxide. After 120min, water vapor was slowly introduced to raise the dew point from 6deg.C to 16deg.C (relative humidity from about 30% to about 60%), and after 60min the carbon dioxide concentration level in the sample chamber gradually increased to 456ppm, indicating that the wet coating layer had the ability to release ("exhale") carbon dioxide. That is, the coating layer has a function of achieving carbon dioxide "breathing" by dry-wet alternation.\|[0072] To sum up: the invention provides a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the water medium carbon dioxide capturing surface layer coating is mainly composed of polystyrene quaternary ammonium salt resin (mass portion 10-15), hydrotalcite-like minerals (mass portion 10-15), diatomite (mass portion 3-5), calcium silicate (mass portion 17-25), rock wool fibers (mass portion 3-5) and dilute cement paste (mass portion 35-57) according to a certain mass mixing proportion, the coating is smeared on the surface of a building, carbon dioxide can be automatically captured from air when a coating layer is dried, carbon dioxide can be desorbed by the coating layer and dissolved in water in a carbonate form to flow out when the coating layer is wet, the carbon dioxide in the air is automatically captured by taking water as a medium, and the carbon dioxide breathing function of the outer facade of the building can be realized.\|[0073] The technical features of the above embodiments may be arbitrarily combined, and all possible combinations of the technical features in the above embodiments are not described for brevity of description, however, as long as there is no contradiction between the combinations of the technical features, they should be considered as the scope of the description.\|[0074] The above embodiments are merely illustrative of the principles of the present invention and its effectiveness, and are not intended to limit the invention. Modifications and variations may be made to the above-described embodiments by those skilled in the art without departing from the spirit and scope of the invention. Accordingly, it is intended that all equivalent modifications and variations of the invention be covered by the claims, which are within the ordinary skill of the art, be within the spirit and scope of the present disclosure.	(CN116463001)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of carbon capture, in particular to a water-medium carbon dioxide capture surface layer coating and a preparation method thereof.\|BACKGROUND ART\|[0002] The capture and sequestration (CCS) of high concentration CO 2 emitted by point sources during the transition period may reduce the emissions of CO 2. However, the aim of stabilizing the CO 2 in the atmosphere below 450ppm is not possible with CCS alone. The concentration of carbon dioxide in air has increased from around 200ppm before the industrial revolution to over 400ppm at present, and therefore, the development of technology for directly capturing carbon dioxide from the surrounding air is also an effective means for slowing down climate change and is urgent.\|DISCLOSURE\|Disclosure of Invention\|[0003] The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried; when the air is wet, carbon dioxide in the gaps of the coating layer is converted into carbonate or bicarbonate to be released, and the carbonate or bicarbonate is flushed with water to enter the water body, so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled, and the problems in the background art are solved.\|[0004] In order to achieve the above purpose, the present invention provides the following technical solutions:\|[0005] A preparation method of water medium carbon dioxide capturing surface layer coating comprises polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion; wherein the mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the paint is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; the mass ratio of the dilute cement paste in the paint is 35-57%. \|[0006] Furthermore, the polystyrene quaternary ammonium salt resin is a main component for capturing carbon dioxide in a water medium, and can be prepared by adopting commercial powder particles or self-preparation, and the particle size is 0.2-1.0mm.\|[0007] Further, the preparation method of the polystyrene quaternary ammonium salt resin comprises the following steps:\|[0008] s1: completely immersing 10 parts of chloromethyl polystyrene resin powder in N, N-Dimethylformamide (DMF) according to the mass ratio, and swelling for 24 hours at 30-40 ℃; \|[0009] s2: adding 2 parts of polyethylenimine, and soaking for 12 hours at 30-40 ℃; \|[0010] s3: soaking in ethanol for 12 hours, filtering and drying; \|[0011] S4: swelling with isopropanol for 24 hours, adding 5 parts of 1 bromododecane for quaternization at 80-85 ℃ for 24 hours, and then adding 1.5 parts of 1 bromobutane for intensive quaternization at 45-50 ℃ for 4 hours; \|[0012] s5: and finally, filtering at room temperature, washing with ethanol and drying to obtain the quaternary ammonium salt modified polystyrene resin powder particles. \|[0013] Further, the hydrotalcite-like mineral is a layered double metal hydroxide composed of Ca/Al/Mg metal oxide, which is derived from natural hydrohead ore, and is assembled by non-covalent bond interaction between positively charged octahedral host laminates and interlayer anions, and has a particle size ranging from 0.1 to 1.0mm.\|[0014] Furthermore, the diatomite is in a powder shape, the particle size is 0.5-1.0mm, and the huge specific surface area of the diatomite particles is beneficial to the adsorption and exchange of gas.\|[0015] Furthermore, the particle size range of the calcium silicate particles is 0.1-0.5mm, and the relative density is 2.5-3.0, so that the calcium silicate has the functions of flame retardance, heat preservation, heat insulation, antibiosis and mildew prevention.\|[0016] Furthermore, the rock wool fiber is common rock wool fiber and is used for increasing the void ratio of the coating and facilitating gas exchange.\|[0017] Still further, the method includes:\|[0018] Mixing dilute cement paste with the water cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers according to a certain mass ratio, and uniformly stirring to obtain a directly-smeared coating; or (b) \|[0019] The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray coating type paint is obtained.\|[0020] Furthermore, the prepared surface layer coating can be directly and uniformly coated or sprayed on the outer surface of the structure, the thickness of the coating is 0.2-0.5cm, and the carbon respiration function of the outer surface of the structure can be realized, namely, carbon dioxide is absorbed when air is gradually dried, and carbon dioxide is released when the air is wet.\|[0021] Compared with the prior art, the invention has the beneficial effects that:\|[0022] The invention provides a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the water medium carbon dioxide capturing surface layer coating is mainly composed of polystyrene quaternary ammonium salt resin (mass portion 10-15), hydrotalcite-like minerals (mass portion 10-15), diatomite (mass portion 3-5), calcium silicate (mass portion 17-25), rock wool fibers (mass portion 3-5) and dilute cement paste (mass portion 35-57) according to a certain mass mixing proportion, the coating is smeared on the surface of a building, carbon dioxide can be automatically captured from air when a coating layer is dried, carbon dioxide can be desorbed by the coating layer and dissolved in water in a carbonate form to flow out when the coating layer is wet, the carbon dioxide in the air is automatically captured by taking water as a medium, and the carbon dioxide breathing function of the outer facade of the building can be realized. \|[0023] The conception, specific structure, and technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, features, and effects of the present invention.\|DRAWINGS DESCRIPTION\|[0024] The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate embodiments of the application and together with the description serve to explain the application.\|[0025] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for the description of the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0026] FIG. 1 is a schematic illustration of the carbon dioxide absorption and release process mechanism of the coating of the present invention;\|[0027] FIG. 2 is a schematic illustration of the application of the coating of the present invention to a facade of a structure; \|[0028] FIG. 3 is a schematic diagram of hydrotalcite-like minerals according to the present invention. \|INVENTION MODE\|Detailed Description\|[0029] Other advantages and effects of the present invention will become apparent to those skilled in the art from the following disclosure, which describes the embodiments of the present invention with reference to specific examples. The invention may be practiced or carried out in other embodiments that depart from the specific details, and the details of the present description may be modified or varied from the spirit and scope of the present invention. It should be noted that the following embodiments and features in the embodiments may be combined with each other without conflict.\|[0030] It should be noted that the illustrations provided in the following embodiments merely illustrate the basic concept of the present invention by way of illustration, and only the components related to the present invention are shown in the illustrations, not according to the number, shape and size of the components in actual implementation, and the form, number and proportion of each component in actual implementation may be arbitrarily changed, and the layout of the components may be more complex.\|[0031] Some exemplary embodiments of the invention have been described for illustrative purposes, it being understood that the invention may be practiced otherwise than as specifically shown in the accompanying drawings.\|[0032] The embodiment of the invention provides a preparation method of a water medium carbon dioxide capturing surface layer coating, which consists of polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion.\|[0033] The polystyrene quaternary ammonium salt resin is a main component for realizing carbon dioxide capture of a water medium, can be prepared from commercial powder particles with the particle size of 0.2-1.0mm, has the mass ratio of 10-15% in the coating, and has a certain mildew-proof and bactericidal effect and is beneficial to mildew prevention of the coating.\|[0034] The preparation method of the polystyrene quaternary ammonium salt resin comprises the following steps:\|[0035] s1: completely immersing 10 parts of chloromethyl polystyrene resin powder in N, N-Dimethylformamide (DMF) according to the mass ratio, and swelling for 24 hours at 30-40 ℃; \|[0036] s2: adding 2 parts of polyethylenimine, and soaking for 12 hours at 30-40 ℃; \|[0037] s3: soaking in ethanol for 12 hours, filtering and drying; \|[0038] S4: swelling with isopropanol for 24 hours, adding 5 parts of 1 bromododecane for quaternization at 80-85 ℃ for 24 hours, and then adding 1.5 parts of 1 bromobutane for intensive quaternization at 45-50 ℃ for 4 hours; \|[0039] s5: and finally, filtering at room temperature, washing with ethanol and drying to obtain the quaternary ammonium salt modified polystyrene resin powder particles. \|[0040] The synthetic process route of the polystyrene quaternary ammonium salt resin is as follows:\|[0041] \|[0042] In the embodiment of the invention, the hydrotalcite-like mineral is mainly a layered double metal hydroxide formed by Ca/Al/Mg metal oxide, is derived from natural hydrofluorite, is assembled by non-covalent bond interaction between a main body laminate of an octahedron (calcoxy, magnesia octahedron or alumina octahedron) with positive charges and an interlayer anion, and has a structure shown in figure 3 (wherein M represents Ca, al or Mg; A represents an anion). \|[0043] In order to reduce cost, natural hydrotalcite-like minerals can be directly adopted, the particle size range of the hydrotalcite-like minerals is 0.1-1.0mm, and the mass ratio of the hydrotalcite-like minerals in the paint is 10-15%.\|[0044] Specifically, hydrotalcite-like minerals can be purchased from the following web sites:\|[0045] aluminum magnesium hydrotalcite (Tianjin balance blue sea technology limited): \|[0046] https://detail.1688.com/offer/661622986146.htmlexp=enquiry%3AB&spm=a312h.2018_new_sem.dh_002.4.753e4b3dwFlIOj&cosite=baidujj&tracelog=p4p&_p_isad=1&clickid=d03616eec8864d809dce520d1839c01d&sessionid=cfdd5b610ea8464e0d77c3b1871a9264&a=1416&e=KWo.0gR-IlmQgV3XCjgNJ7LfaupOvlS.jc7eTz15fCH9PqbBDDQSDzB3m4XMOgA2e2OtVP1Jh4sb7AJCzkOHH5ZgSgUQMMbOH9p4ldzbdqEkTW.VtH..9uIaYQ4Zs.dt.o8k8junxwtz3zM49yD9eKsE2ZV6JcpvnCOJLKxPYQ96Hg0R6Cv1gtCPyb20.DQ8nuhLQNZ9dqHjqfl.RGtZYkVHyVZEqONRqtYzmCIrysY3GBxjBoOQaM5Jy6mnZopXvloJuMZHzzi885SgK3ZLXw__&sk=sem&style=1.\|[0047] aluminum magnesium hydrotalcite (Jin Shuiou Hongyuan chemical industry business, zheng state): \|[0048] https://detail.1688.com/offer/588588278288.html&idx=50。\|[0049] Aluminum-calcium hydrotalcite (Jining Sanshi biotechnology Co., ltd.): \|[0050] https://detail.1688.com/offer/677407307296.html&idx=55。\|[0051] The hydrotalcite-like mineral is helpful for the paint to realize the adsorption and release of carbonate anions and bicarbonate anions. Meanwhile, the hydrotalcite mineral has the capability of absorbing infrared light with specific wavelength, can accelerate the heating and drying of the paint, accelerates the absorption of carbon dioxide by the paint, and is more conducive to the realization of the absorption of infrared wave bands after the hydrotalcite-like mineral is combined with the organic ion exchange resin. \|[0052] The diatomite in the embodiment of the invention is in a powder shape, the particle size is 0.5-1.0mm, the mass fraction is 3-5%, and the huge specific surface area of the diatomite particles is beneficial to the adsorption and exchange of gas.\|[0053] The particle size range of the calcium silicate particles in the embodiment of the invention is 0.1-0.5mm, the relative density is 2.5-3.0, the mass ratio of the calcium silicate particles in the coating is 17-25%, and the calcium silicate can increase the functions of flame retardance, heat preservation, heat insulation, antibiosis and mildew resistance of the surface of a structure.\|[0054] The rock wool fiber in the embodiment of the invention is common basalt rock wool fiber, the mass share of the rock wool fiber is 3-5%, the fiber length is 1-5cm, and the rock wool fiber has the main function of increasing the void ratio of the coating and is beneficial to gas exchange.\|[0055] According to the application mode of the coating, the water-cement ratio of the dilute cement slurry is divided into two types, and the dilute cement slurry with the water-cement ratio of 0.65-0.80, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly stirred according to a certain mass ratio, so that the directly smeared coating is obtained; or alternatively\|[0056] The dilute cement slurry with the water cement ratio of 0.80-1.00, the polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate and rock wool fibers are mixed and uniformly mixed according to a certain mass ratio, and then the spray coating type paint is obtained.\|[0057] The carbon breath of the structure to carbon dioxide can be realized by painting the paint on the outer surface of the structure (the thickness of the coating is 0.2-0.5 cm), namely, carbon dioxide is absorbed when air is gradually dried, and carbon dioxide is released when the air is wet.\|[0058] The research and development principle of the invention: according to prior art documents, materials that successfully achieve direct capture of carbon dioxide from air generally require that 4 conditions be met:\|[0059] (1) Rapid reaction kinetics, and can rapidly absorb carbon dioxide; (2) the cost is low enough to facilitate the development and popularization of the application; (3) the application scene is wide, and large-scale application can be developed; (4) The method is convenient for rapid regeneration under general environmental conditions, and can complete the whole CO 2 capturing-releasing cycle. \|[0060] In practice, however, there are a number of substances that can achieve carbon dioxide adsorption, but it is difficult to achieve regeneration under normal environmental conditions (condition (4) is not satisfied), because they must overcome a large energy barrier to regenerate. For example, the heat of adsorption required for the calcium-based calcination process and the sodium-based decomposition hydrolysis process are 179kJ/mol CO 2 and 135kJ/mol CO 2, respectively, and the amine-based adsorbent has a heat of adsorption for CO 2 of about 80kJ/mol CO 2, respectively. They require a large amount of energy if they need to be released again after adsorbing carbon dioxide, which in turn leads to carbon dioxide emissions.\|[0061] Therefore, the embodiment of the invention provides the energy-saving adsorbent taking water as a medium, carbon dioxide can be captured and released only by means of the water medium in contact with the material, compared with other adsorption materials, the adsorption heat of the ion exchange resin is only 32kJ/mol CO 2, and when the relative humidity of air is increased from 15% to 100%, the equilibrium partial pressure of CO 2 on the polystyrene quaternary ammonium salt ion exchange resin is increased by 2 orders of magnitude, namely, the carbon dioxide adsorbed in the polystyrene quaternary ammonium salt ion exchange resin is obviously released due to the increase of the air humidity. This effect is due on the one hand to the physical competitive adsorption of water vapor and carbon dioxide by the polystyrene quaternary ammonium ion exchange resin and on the other hand to the good affinity of the polystyrene quaternary ammonium ion exchange resin for CO 2 when dried.\|[0062] The principle of the polystyrene quaternary ammonium salt ion exchange resin is as follows: with the air-drying process in-line with the air-drying process, The positively charged adsorbed CO 32- in the quaternary ammonium salt and water molecules in the material gaps are converted into HCO 3-, Thereby freeing up an adsorption site for the absorption of OH -, while OH - absorbs CO 2 from the air and converts it to HCO 3-, the process thus achieves direct capture of carbon dioxide in the air; when the air is wet, the air is in contact with the air, The 2 HCO 3- are combined and converted into CO 32- and CO 2 are carried away by water, Part of CO 32- occupies 2 positive charge adsorption sites in the quaternary ammonium salt. I.e., adsorption/desorption of CO 2, can be expressed as a series of reactions: dissociation of water, formation of bicarbonate, adsorption of CO 2 on hydroxide, release of carbonate from bicarbonate back and release of CO 2. The main chemical process is shown in the following formula and is shown in the attached figure 1.\|[0063] H2O=H++OH-\|[0064] CO32-+H+=HCO3-\|[0065] OH-+CO2=HCO3-\|[0066] HCO3-+HCO3-=CO32-+CO2+H2O\|[0067] In order to meet 4 conditions of successfully realizing direct capture of carbon dioxide materials from air, the embodiment of the invention provides a water medium carbon dioxide capture surface layer coating and a preparation method thereof. Mainly comprises polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, diatomite, calcium silicate, rock wool fibers and dilute cement slurry according to a certain mass mixing proportion.\|[0068] For further better explanation of the invention, the following specific embodiments are provided:\|[0069] 10 g of polystyrene quaternary ammonium salt ion exchange resin balls (particle size of 0.5 mm), 10 g of hydrotalcite mineral particles (particle size of 0.5 mm), 3 g of diatomite particles (particle size of 0.5-1.0 mm), 17 g of calcium silicate (particle size of 0.5 mm), 3 g of rock wool fibers (basalt fibers for common insulation boards) and 57 g of dilute cement paste (water cement ratio of 0.75) are mixed, firstly, manual pre-mixing is carried out, then the mixture is put into a beaker, and mechanical mixing is carried out for 30min by using a dispersing machine, and the stirring speed is 18-22r/min. About 100 grams of coating was finally obtained. \|[0070] As shown in FIG. 2, a portion of the coating was spread on a 10cm by 10cm tile surface to a thickness of 0.5mm and then dried in a vacuum oven at 105℃for 24 hours to ensure complete drying of the coating, which removed carbon dioxide and moisture incorporated within the coating. The tile is then quickly placed in a sample cell (30 cm x 30cm closed plexiglass box) that is connected to an infrared gas analyzer LICOR840, and the carbon dioxide concentration and dew point (the greater the relative humidity, the higher the dew point temperature) of the sample cell can be obtained in real time.\|[0071] As can be seen by instrumental observation, the concentration of carbon dioxide in the sample chamber was reduced from 800ppm to 400ppm over 60min and to 320ppm over 120min after the dried tile coated with the coating was placed, indicating that the dried coating layer had the ability to absorb ("call in") carbon dioxide. After 120min, water vapor was slowly introduced to raise the dew point from 6deg.C to 16deg.C (relative humidity from about 30% to about 60%), and after 60min the carbon dioxide concentration level in the sample chamber gradually increased to 456ppm, indicating that the wet coating layer had the ability to release ("exhale") carbon dioxide. That is, the coating layer has a function of achieving carbon dioxide "breathing" by dry-wet alternation.\|[0072] To sum up: the invention provides a water medium carbon dioxide capturing surface layer coating and a preparation method thereof, wherein the water medium carbon dioxide capturing surface layer coating is mainly composed of polystyrene quaternary ammonium salt resin (mass portion 10-15), hydrotalcite-like minerals (mass portion 10-15), diatomite (mass portion 3-5), calcium silicate (mass portion 17-25), rock wool fibers (mass portion 3-5) and dilute cement paste (mass portion 35-57) according to a certain mass mixing proportion, the coating is smeared on the surface of a building, carbon dioxide can be automatically captured from air when a coating layer is dried, carbon dioxide can be desorbed by the coating layer and dissolved in water in a carbonate form to flow out when the coating layer is wet, the carbon dioxide in the air is automatically captured by taking water as a medium, and the carbon dioxide breathing function of the outer facade of the building can be realized.\|[0073] The technical features of the above embodiments may be arbitrarily combined, and all possible combinations of the technical features in the above embodiments are not described for brevity of description, however, as long as there is no contradiction between the combinations of the technical features, they should be considered as the scope of the description.\|[0074] The above embodiments are merely illustrative of the principles of the present invention and its effectiveness, and are not intended to limit the invention. Modifications and variations may be made to the above-described embodiments by those skilled in the art without departing from the spirit and scope of the invention. Accordingly, it is intended that all equivalent modifications and variations of the invention be covered by the claims, which are within the ordinary skill of the art, be within the spirit and scope of the present disclosure.	Family Number\|(100341084)\|100341084\|Object of Invention\|(CN114574045 A)\|The invention aims to provide a preparation method of a water - borne carbon dioxide capturing surface layer coating , which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried ; when the air is wet , carbon dioxide in the gaps of the coating ( . . . ) carbonate or bicarbonate to be released and then enters the water body along with water washing , so that the purpose of directly capturing carbon dioxide from the air and transferring the carbon dioxide to the water body is achieved , and the problems in the background art are solved . \|The invention discloses a preparation method of a water - borne carbon dioxide capturing surface layer coating , which is formed by mixing polystyrene quaternary ammonium salt resin ( 10-15 mass portions ) , hydrotalcite - like ( . . . ) the coating can desorb the carbon dioxide and is dissolved in water to flow out , water is used as a medium , the automatic capture of the carbon dioxide in the air is realized , and the carbon breathing function of the outer vertical surface of the building can be realized . The invention relates to the technical field of carbon capture , in particular to a preparation method of a surface coating for capturing carbon dioxide in a water medium . \|the invention provides a preparation method of a water - borne carbon dioxide capture surface layer coating , which is mainly composed of polystyrene quaternary ammonium salt resin ( mass portion 10-15 ) , hydrotalcite - like ( . . . ) the carbon dioxide in the form of carbonate in water to flow out , the device takes water as a medium , realizes automatic capture of carbon dioxide in the air , and can realize the carbon breathing function of the outer facade of the structure . \|(CN116463001 A)\|The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof , which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried ; when the air is wet , carbon dioxide in the gaps of the coating ( . . . ) be released , and the carbonate or bicarbonate is flushed with water to enter the water body , so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled , and the problems in the background art are solved . \|The invention discloses a water medium carbon dioxide capturing surface layer coating and a preparation method thereof , wherein the coating is composed of polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; the mass ratio of the polystyrene quaternary ammonium salt resin in the paint is 10-15% ; the mass ratio of hydrotalcite - like minerals in the paint is 10-15% ; ( . . . ) \|The invention relates to the technical field of carbon capture , in particular to a water - medium carbon dioxide capture surface layer coating and a preparation method thereof . \|(CN116463001B B)\|The invention aims to provide a water medium carbon dioxide capturing surface layer coating and a preparation method thereof , which can directly and strongly adsorb and capture carbon dioxide from air into a coating layer when the air is dried ; when the air is wet , carbon dioxide in the gaps of the coating ( . . . ) be released , and the carbonate or bicarbonate is flushed with water to enter the water body , so that the aim of directly capturing carbon dioxide from the air and transferring the carbon dioxide into the water body is fulfilled , and the problems in the background art are solved . \|The invention discloses a water medium carbon dioxide capturing surface layer coating and a preparation method thereof , wherein the coating is composed of polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; the mass ratio of the polystyrene quaternary ammonium salt resin in the paint is 10-15% ; the mass ratio of hydrotalcite - like minerals in the paint is 10-15% ; ( . . . ) \|The invention relates to the technical field of carbon capture , in particular to a water - medium carbon dioxide capture surface layer coating and a preparation method thereof . \|Abstract\|(CN114574045 A)\|The invention discloses a preparation method of a water medium carbon dioxide capture surface coating . The coating is formed by mixing 10-15 parts by mass of polystyrene quaternary ammonium salt resin , 10-15 parts by mass of hydrotalcite - like minerals , 3-5 parts by mass of diatomite , 17-25 parts by mass of calcium silicate , 3-5 parts by mass of rock wool fibers and 35-57 parts by mass of thin cement paste according to a certain mass ratio , the coating is smeared on the surface of a building , and when a coating layer is dried , the coating layer is coated on the surface of the building . When the coating layer is wet , the coating layer can desorb the carbon dioxide and dissolve the carbon dioxide in water in a carbonate form to flow out , water serves as a medium , automatic capture of the carbon dioxide in the air is achieved , and the carbon breathing function of the outer vertical face of a building can be achieved . \|(CN116463001B B)\|The invention discloses a water medium carbon dioxide capture surface coating and a preparation method thereof . The water medium carbon dioxide capture surface coating is formed by mixing polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , kieselguhr , calcium silicate , rock wool fibers and thin cement paste according to a certain mass ratio . The mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15% ; the mass ratio of the hydrotalcite - like mineral in the coating is 10-15% ; the mass ratio of the diatomite in the coating is 3-5% ; the mass ratio of the calcium silicate in the coating is 17-25% ; the mass ratio of the rock wool fibers in the coating is 3-5% ; and the mass ratio of the thin cement paste in the coating is 35-57%. The coating is smeared on the surface of a building , and when a coating layer is dry , carbon dioxide can be automatically captured from air ; when the coating layer is wet , the coating layer can desorb carbon dioxide and dissolve the carbon dioxide in water in a carbonate form to flow out , so that the carbon breathing function of the external facade of the building is realized . \|Title\|(CN114574045 A)\|Preparation method of water medium carbon dioxide capture surface coating \|(CN116463001 A)\|Water medium carbon dioxide capture surface coating and preparation method thereof \|(CN116463001B B)\|Water medium carbon dioxide capturing surface layer coating and preparation method thereof \|Independent Claims\|(CN114574045 A)\|1. The preparation method of the water - borne carbon dioxide capturing surface coating is characterized by comprising polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement paste according to a certain mass mixing ratio . \|(CN116463001 A)\|1. The preparation method of the water medium carbon dioxide capturing surface layer coating is characterized by comprising polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; \|10. The water medium carbon dioxide capturing surface layer coating is characterized by being composed of polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; \|(CN116463001B B)\|1. The preparation method of the water medium carbon dioxide capturing surface layer coating is characterized by comprising polystyrene quaternary ammonium salt resin , hydrotalcite - like minerals , diatomite , calcium silicate , rock wool fibers and dilute cement slurry according to a certain mass mixing proportion ; ( . . . ) \|	Basic materials chemistry	C09D-001/08\|C09D-007/61\|C09D-007/65\|C09D-007/70\|Y02C-020/40		C09D-001/08\|C09D-007/61\|C09D-007/65\|C09D-007/70\|Y02C-020/40	C09D-001/08\|C09D-007/61\|C09D-007/65\|C09D-125/06	C09D-001/08\|C09D-007/61\|C09D-007/65\|C09D-125/06			CN116463001B	CN116463001B 100341084 WHO=Examiner SELF=Y	CN113680334\|CN109575659\|CN108622951\|CN108043368\|CN107699089\|CN104056599\|CN103540199\|CN103958027\|KR20120028044\|CN114574045\|US20160229760	CN113680334 97148868 WHO=Examiner SELF=N CAT=A\|CN109575659 84062764 WHO=Examiner SELF=N CAT=A\|CN108622951 81572593 WHO=Examiner SELF=Y CAT=A\|CN108043368 79763962 WHO=Examiner SELF=N CAT=A\|CN107699089 78837473 WHO=Examiner SELF=N CAT=A\|CN104056599 67501607 WHO=Examiner SELF=N CAT=A\|CN103540199 59588170 WHO=Examiner SELF=N CAT=A\|CN103958027 94752751 WHO=Examiner SELF=N CAT=A\|KR20120028044 35317232 WHO=Examiner SELF=N CAT=A\|CN114574045 100341084 WHO=Examiner SELF=Y\|US20160229760 73830880 WHO=Examiner SELF=N	侯成龙: "季铵修饰聚合物的制备及空气二氧化碳捕集性能研究", 中国优秀博士学位论文全文数据库工程科技1辑, no. 1, pages 014 - 214 (Cat. Y)\|程磊: "氯甲基聚苯乙烯树脂接枝聚季铵盐型杀菌剂的制备及其杀菌性能", 石油化工, vol. 39, no. 1, pages 75 - 80 (Cat. Y)\|季铵修饰聚合物的制备及空气二氧化碳捕集性能研究;侯成龙;中国优秀博士学位论文全文数据库工程科技1辑(第第1期期);第B014-214页 (Cat. Y)\|氯甲基聚苯乙烯树脂接枝聚季铵盐型杀菌剂的制备及其杀菌性能;程磊;石油化工;第第39卷卷(第第1期期);第75-80页 (Cat. Y)\|滕巧巧: "“聚苯乙烯接枝聚乙烯亚胺树脂合成及Cu2+吸附”", 《化工进展》 (Cat. A)\|程磊等: "“氯甲基聚苯乙烯树脂接枝聚季铵盐型杀菌剂的制备及其杀菌性能”", 《石油化工》 (Cat. A)	KR20120028044; CN103958027; CN114574045; US20160229760\|CN103540199; CN104056599; CN107699089; CN108043368; CN108622951; CN109575659; CN113680334		GRANTED	(CN116463001)\|GRANTED\|(CN114574045)\|LAPSED	ALIVE	(CN116463001)\|ALIVE\|(CN114574045)\|DEAD	(CN116463001)\|LEGAL DETAILS FOR CN116463001\|Actual or expected expiration date=2043-03-15\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2023-03-15\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202310250007\|Application date=2023-03-15\|Standardized application number=2023CN-0250007\|Event publication date=2023-07-21\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN116463001\|Publication stage code=A\|Publication date=2023-07-21\|Standardized publication number=CN116463001\|Event publication date=2023-07-21\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2023-08-15\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2024-07-05\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN116463001\|Publication stage code=B\|Publication date=2024-07-05\|Standardized publication number=CN116463001B\|Event publication date=2024-07-05\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|(CN114574045)\|LEGAL DETAILS FOR CN114574045\|Actual or expected expiration date=2023-08-29\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-03-18\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202210271537\|Application date=2022-03-18\|Standardized application number=2022CN-0271537\|Event publication date=2022-06-03\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN114574045\|Publication stage code=A\|Publication date=2022-06-03\|Standardized publication number=CN114574045\|Event publication date=2022-06-03\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2022-06-21\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2023-08-29\|Event code=CN/WD01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent application deemed withdrawn after publication		(CN116463001)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQB4wlV1sYkERj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000073463133&ekey=2216&xpn=CN116463001B&kind=B	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=%252FUHDmbKj7zr%252Br9sAuSz3o7msLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN116463001)\|CN\|(CN116463001)\|CN\|(CN114574045)\|CN	(CN116463001)\|NAME=SHANGHAI ZEYAO ENV PROT TECH CO LTD , COUNTRY=CN\|(CN116463001)\|NAME=SHANGHAI ZEYAO ENV PROT TECH CO LTD , COUNTRY=CN\|(CN114574045)\|NAME=SHANGHAI ZEYAO ENV PROT TECH CO LTD , COUNTRY=CN		(CN116463001)\|NAME=XU HAOJUN;SHANGHAI JIANQIU INTELLECTUAL PROPERTY ATTORNEYS , REG=31382\|(CN116463001)\|NAME=XU HAOJUN;SHANGHAI JIANQIU INTELLECTUAL PROPERTY ATTORNEYS , REG=31382\|(CN114574045)\|NAME=HE XINXIN;Hefei Du Lei Intellectual Property Agency (General Partnership) , REG=34227		(CN116463001)\|NAME=Song Xinshan\|NAME=Xu Yong\|NAME=Zhang Zhilan\|NAME=Wang Yuhui\|NAME=Xu Zhongshuo\|NAME=Wang Yifei\|NAME=Liu Yingying\|NAME=Tan Shujuan\|NAME=Huang Na\|NAME=Tang Haiyan\|(CN116463001)\|NAME=SONG XINSHAN\|NAME=XU YONG\|NAME=ZHANG ZHILAN\|NAME=WANG YUHUI\|NAME=XU ZHONGSHUO\|NAME=WANG YIFEI\|NAME=LIU YINGYING\|NAME=TAN SHUJUAN\|NAME=HUANG NA\|NAME=TANG HAIYAN\|(CN114574045)\|NAME=SONG XINSHAN\|NAME=XU YONG\|NAME=ZHANG ZHILAN\|NAME=WANG YUHUI\|NAME=XU ZHONGSHUO\|NAME=WANG YIFEI\|NAME=LIU YINGYING\|NAME=TAN SHUJUAN\|NAME=HUANG NA\|NAME=TANG HAIYAN	(CN116463001)\|3\|(CN114574045)\|2	1	2					(CN116463001)\|Number of Claims: NCL=7\|Gazette date: GAZDATE=2024-07-05\|Gazette number: GAZNUM=40-2702\|Number of Pages: NPAGES=10\|Primary examiner: 赵欢\|Primary examiner: Zhao Huan\|\|(CN116463001)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2023-07-21\|Gazette number: GAZNUM=39-2902\|Number of Pages: NPAGES=11\|Primary examiner: 赵欢\|Primary examiner: Zhao Huan\|\|(CN114574045)\|Number of Claims: NCL=9\|Gazette date: GAZDATE=2022-06-03\|Gazette number: GAZNUM=38-2202\|Number of Pages: NPAGES=9\|	(CN116463001)\|Previous publication: CN116463001 A 2023-07-21 [CN116463001]	(CN116463001)\|CHINESE (CHI)	(CN116463001B)\|Patent\|(CN116463001)\|Patent\|(CN114574045)\|Patent	Titre: (CN116463001)\|Water medium carbon dioxide capturing surface layer coating and preparation method thereof Résumé: (CN116463001)\|The invention discloses a water medium carbon dioxide capture surface coating and a preparation method thereof. The water medium carbon dioxide capture surface coating is formed by mixing polystyrene quaternary ammonium salt resin, hydrotalcite-like minerals, kieselguhr, calcium silicate, rock wool fibers and thin cement paste according to a certain mass ratio. The mass ratio of the polystyrene quaternary ammonium salt resin in the coating is 10-15%; the mass ratio of the hydrotalcite-like mineral in the coating is 10-15%; the mass ratio of the diatomite in the coating is 3-5%; the mass ratio of the calcium silicate in the coating is 17-25%; the mass ratio of the rock wool fibers in the coating is 3-5%; and the mass ratio of the thin cement paste in the coating is 35-57%. The coating is smeared on the surface of a building, and when a coating layer is dry, carbon dioxide can be automatically captured from air; when the coating layer is wet, the coating layer can desorb carbon dioxide and dissolve the carbon dioxide in water in a carbonate form to flow out, so that the carbon breathing function of the external facade of the building is realized.	9	Abstract	gpt-4o-mini	no	The article focuses on a surface coating for capturing CO₂ from the air, which does not involve the accelerated weathering of minerals or the specific processes related to mineral carbonation for carbon sequestration.
12	IN202441017388	IN202441017388	IN202441017388	116031041	IN202441017388 A 2025-09-12 [IN202441017388]	2024-03-11	2024-03-11	2025-09-12		(IN202441017388)\|2044-03-11	(IN202441017388)\|System and method for preparing carbonate-enhanced nutrition composition using geo-bags	(IN202441017388)\|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112. The system includes a rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The reactor 108 mixes crushed rocks and organic acid components to prepare a carbon-sequestration substrate. The geo-bag 112 is filled with the carbon-sequestration substrate, and the geo-bag 112 is made from eco-friendly materials, allowing selective exchange of components between the bag contents and the environment. The substrate in the geo-bag 112 is allowed to capture the CO2 from the atmosphereand convert the carbon-sequestration substrate into a carbonateenhanced nutrition composition, thereby reducing the environmental CO2 level. The composition includes high economic value materials like calcium carbonate, potash, phosphate, and heavy metals. The composition can be used as a fertilizer or building construction material like M-sand.	HYPERWORKS IMAGING PRIVATE	(IN202441017388)\|HYPERWORKS IMAGING PRIVATE LIMITED	Tannirkulam Ajay\|Margankunte Naveen	(IN202441017388)\|Tannirkulam Ajay\|Margankunte Naveen			(IN202441017388)\|1. A method for preparing a carbonate-enhanced nutrition composition using a geo-bag (112) wherein the method comprising: i) Collecting and crushing rocks into small particles, using a rock crushing unit (102); ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbon-sequestration substrate, using a reactor (108) by Characterized in that, a) mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions; and b) filling the carbon-sequestration substrate into the geo-bag (112) to prepare carbon-sequestration packages, wherein the geo-bag (112) comprises an ecofriendly material that permits only water and air to pass through while retaining the substrate inside, wherein the geo-bag (112) comprises a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbonsequestration substrate by subjecting the carbon-sequestration packages to a rockcarbonation period at an operating location to capture atmospheric carbon dioxide; wherein the geo-bag (112) acts as a structural member providing a high surface area-tovolume ratio to optimize carbon dioxide capture resulting 15 to 130 times enhanced carbonation efficiency.\|	(IN202441017388)\|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112.\|Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.\|	(IN202441017388)\|GEOBAG(100,42)\|CARBONATE ENHANCED NUTRITION(100,29)\|ROCK CRUSHING(57,8)\|CARBONSEQUESTRATION SUBSTRATE(48,2)\|CARBON SEQUESTRATION SUBSTRATE(44,31)\|ENHANCED CARBONATION(44,3)\|URBAN ORGANIC WASTAGE COLLECTION(41,4)\|CARBON SEQUESTRATION(37,42)\|ROCK CARBONATION PERIOD(35,9)\|MIX CRUSHED ROCK(33,1)\|CARBON DIOXIDE CAPTURE(32,1)\|GRAVEL(31,21)\|BIOMASS(28,12)\|CARBON SEQUESTRATION PACKAGE(26,8)\|SUBSTRATE INSIDE(26,1)\|MIXING CONDITION(24,6)\|FERTILIZER(24,4)\|ATMOSPHERIC CARBON DIOXIDE(24,2)\|ECOFRIENDLY MATERIAL(24,1)\|REACTOR(23,14)\|OUTDOOR ENVIRONMENT(23,4)\|BAG CONTENT(20,3)\|ORGANIC ACID EXTRACTION(19,8)\|ACETIC ACID COMPOUND(18,2)\|POTASH(17,6)\|GEOTEXTILE(17,4)\|MOISTURE CONTENT(17,4)\|AGRICULTURE(16,2)\|CARBON DIOXIDE(15,17)\|CALCIUM CARBONATE(15,6)\|DECOMPOSITION(15,3)\|MICROALGAE(15,3)\|CO2 LEVEL(15,2)\|OLIVINE(14,3)\|VOLUME RATIO(14,2)\|ACETIC ACID(13,8)\|ROCK CRUSHER(13,3)\|STONE WEIGHT(11,4)\|PH VALUE RANGING(11,3)\|ACCELERATE WEATHERING(11,2)\|CELLULOSE DERIVED MONOSACCHARIDE(11,2)\|CONCENTRATION LEVEL RANGING(11,2)\|HDPE(11,2)\|MAGNESIUM CARBONATE(11,2)\|SMALL PARTICLE(10,6)\|TRANSPORTATION MEDIUM(10,5)\|ECO FRIENDLY MATERIAL(10,4)\|BUILDING CONSTRUCTION(10,1)\|CARBONATED ENHANCED NUTRITION(10,1)\|THANTHE NATURAL CARBONATION(10,1)\|TOA CARBON MINERALIZATION(10,1)\|MIXING TEMPERATURE(9,4)\|SUPERCRITICAL CONDITION(9,4)\|DUNITE ANALYSIS(9,3)\|ELECTRO MICROBIAL PRODUCTION(9,2)\|REFILL CARTRIDGE(9,2)\|ROCK CARBONATION PERIOD RANGE(9,2)\|BASALT IC ROCK(9,1)\|LIQUEFIED BIOMASS CONVERSION(9,1)\|ORGANIC ACID COMPONENT(8,18)\|CONDITION OPTIMIZATION(8,6)\|EXPERIMENTAL SETUP(8,2)\|LIQUEFACTION REACTION(8,2)\|ACCELERATE CARBONATION(8,1)\|BIOMASS LIQUEFACTION(8,1)\|CONE CRUSHING(8,1)\|MINERAL DISSOLUTION REACTOR(8,1)\|STONE SIZE(7,12)\|CARBONIZATION(7,11)\|HEAVY METAL(7,6)\|CARBONATION MENSTRUATION(7,3)\|FURFURAL ACID LACTIC(7,3)\|STRUCTURAL MEMBER(7,3)\|VALUED MATERIAL(6,8)\|PPM(6,4)\|DIKETO GLUCONIC ACID(6,2)\|NONOPTIMIZED CONDITION(6,2)\|SAND SPRAY(6,2)\|BURIED FORA(6,1)\|CARBONATION REACTOR(6,1)\|CRUSHED ROCK RETRIEVAL(6,1)\|FARMING LAND(6,1)\|FEEDER BREAKER(6,1)\|MITIGATE ISSUE(6,1)\|NUTRITION ENHANCEMENT(6,1)\|RAW BASALT SAMPLE(6,1)\|RAW DUNITE SAMPLE(6,1)\|ATMOSPHERIC PRESSURE(5,4)\|CONSTRUCTION SITE(5,3)\|TRAPPING(5,3)\|BALL MILL CRUSHER(5,1)\|BASALT ANALYSIS(5,1)\|CARBONATION PERFORMANCE(5,1)\|DIKETOGLUCONIC ACID(5,1)\|DUNITEROCK SAMPLE(5,1)\|FEEDING ROCK(5,1)\|OPTIMIZED CARBONATION CONDITION(5,1)\|URBAN ORGANIC WASTE COLLECTION(5,1)\|FILLING STATION(4,4)\|GRAPHICAL REPRESENTATION(4,4)\|WEIGHT VOLUME(4,4)\|FIBER DENSITY(4,2)\|SOLID MINERAL(4,2)\|SYSTEM COMPLICATION(4,2)\|ASTHE REACTED CARBON REMAINS(4,1)\|BIO CATALYST COMBINATION(4,1)\|CARBON DIOXIDE SEQUESTRATION(4,1)\|CARBONATE ENHANCED MINERAL FORMATION(4,1)\|CARBONSEQUESTRATION(4,1)\|CO MINERALIZATION(4,1)\|DISPENSATION(4,1)\|EXCAVATOR(4,1)\|GYRATORY CRUSHER(4,1)\|OPTIMIZED ENVIRONMENT(4,1)\|PRIMARY COMPARTMENT(4,1)\|SIGNIFICANTRISEINATMOSPHERIC CARBON DIOXIDE(4,1)\|SYSTEMFORPREPARING(4,1)\|	(IN202441017388)\|1. A method for preparing a carbonate-enhanced nutrition composition using a geo-bag (112) wherein the method comprising: i) Collecting and crushing rocks into small particles, using a rock crushing unit (102); ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbon-sequestration substrate, using a reactor (108) by Characterized in that, a) mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions; and b) filling the carbon-sequestration substrate into the geo-bag (112) to prepare carbon-sequestration packages, wherein the geo-bag (112) comprises an ecofriendly material that permits only water and air to pass through while retaining the substrate inside, wherein the geo-bag (112) comprises a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbonsequestration substrate by subjecting the carbon-sequestration packages to a rockcarbonation period at an operating location to capture atmospheric carbon dioxide; wherein the geo-bag (112) acts as a structural member providing a high surface area-tovolume ratio to optimize carbon dioxide capture resulting 15 to 130 times enhanced carbonation efficiency.\|2. The method as claimed in claim 1, wherein the crushed rocks comprise at least one of olivine, dunite, ultramafic, basalt, serpentine, and/or a combination thereof, wherein the crushed rocks comprises of a particle size below 5 mm.\|3. The method as claimed in claim 1, wherein the predefined mixing conditions comprise a mixing temperature ranging from 25°C to 30°C and an atmospheric pressure ranging from 1 atm to 2 atm.\|4. The method as claimed in claim 1, wherein the carbon-sequestration substrate comprises a concentration level ranging from 400 part per million (ppm) to 450 ppm, a moisture content ranging from 25% to 95% of rock weight and has a pH value ranging from 2.5 to 3.5.\|5. The method as claimed in claim 1, wherein the geo-bag (112) comprises at least one of geotextiles, high-density polyethylene (HDPE), and/or a combination thereof.\|6. The method as claimed in claim 1, wherein the rock-carbonation period ranges from 2 years to 5 years.\|7. The method as claimed in claim 1, wherein the organic acid component is extracted using an electro-microbial production (EMP) technique from the biomass; wherein the biomass is generated from the decomposition of at least one of organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof.\|8. The method as claimed in claim 1, wherein the operating location comprises at least one of farming land, a construction site, an outdoor environment.\|9. The method as claimed in claim 1, wherein the method comprises extracting high-value materials from the carbonate-enhanced composition, wherein the high-value materials comprise at least one of magnesium carbonate, calcium carbonate, potash, phosphate, heavy metals and/or a combination thereof.\|10. The method as claimed in claim 1, wherein the carbonate-enhanced composition is used as fertilizer in agriculture and/or as M-sand in the construction field.	(IN202441017388)\|Technical Field\|[0001] The embodiments herein generally relate toa carbon mineralization method, and more particularly, a system and method for preparing carbonate-enhanced nutrition composition using a geo-bag. Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.\|Description of the Related Art\|[0002] In recent years, the significantriseinatmospheric carbon dioxide (CO2) levels has been identified as a leading cause of climate change on Earth. To mitigate this issue, carbon mineralization, or carbon sequestration, has emerged as a prominent method. Carbon mineralization is a process of converting carbon dioxide into solid minerals, such as carbonate, through a chemical reaction. This reaction occurs when specific types of rocks, such as serpentine, basalt, mafic, ultramafic, etc., are exposed to carbon dioxide, resulting in the formation of carbonate-enhanced minerals. Hence, the atmospheric CO2 level is stabilized asthe reacted carbon remains bound within the solid minerals, preventing its release into the atmosphere. However, it is important to note that this process typically requires several years to effectively reduce carbon levels in the atmosphere.\|[0003] Most of the existing carbon sequestration systemsto produce carbonate-enhanced mineralsutilize indoor techniques, employingan indirect method. For example, thesesystemsincludea mineral dissolution reactor for mixing various materials. These materials include magnesium or calcium, which is available in the rocks (e.g. serpentine, olivine, basalt, or labradorite), organic acid, and chelating agents. Through this mixing process, a magnesium or calcium-rich solvent is synthesized tocapture and store carbon dioxide. Additionally, these existing systemsinclude a combined biocatalyst and carbonation reactor, along witha control module for expediting the process of sequestration of carbon. However, the current indoor technique requires a more complicated arrangement and entails higher costs.\|[0004] Accordingly, there remains a need for a more simple and direct approach to capture and store the carbon dioxide from the atmosphere at a reduced economic level and to produce a carbonated enhanced nutrition composition using a geo-bag.\|SUMMARY\|[0005] In view of a foregoing, an embodiment herein provides a method for preparing a carbonate-enhanced nutrition composition using a geo-bag. The method includes i) collecting and crushing rocks into small particles, using a rock crushing unit; ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbonsequestration substrate using a reactor by mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions. The carbon-sequestration substrate is filled into geo-bags to prepare carbon-sequestration packages. The geo-bag includes an eco-friendly material that only permits water and air to pass through while retaining the substrate. The geo-bag consists of a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbon-sequestration substrate by subjecting the carbonsequestration packages to a rock-carbonation period at an operating location to capture atmospheric carbon dioxide. The geo-bag acts as a structural member providing a high surface area-to-volume ratio to optimize carbon dioxide capture resulting in 15 to 130 times enhanced carbonation efficiency.\|[0006] In some embodiments, the crushed rocks include at least one of olivine, dunite, ultramafic, basalt, serpentine, and/or a combination thereof. The crushed rocks include a particle size below 5 mm.\|[0007] In some embodiments, the predefined mixing conditions include a mixing temperature ranging from 25°C to 30°C and an atmospheric pressure ranging from 1 atm to 2\|atm.\|[0008] In some embodiments, the carbon-sequestration substrate includes a concentration level ranging from 400 parts per million (ppm) to 450 ppm, a moisture content ranging from\|25% to 95% of rock weight and a pH value ranging from 2.5 to 3.5.\|[0009] In some embodiments, the geo-bag includes at least one of the geotextiles, highdensity polyethylene (HDPE), and/or a combination thereof.\|[0010] In some embodiments, the rock-carbonation period ranges from 2 years to 5 years.\|[0011] In some embodiments, the organic acid component is extracted using an electromicrobial production (EMP) technique from the biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof.\|[0012] In some embodiments, the operating location includes at least one farming land, a construction site, and an outdoor environment.\|[0013] In some embodiments, the method includes extracting high-value materials from the carbonate-enhanced nutrition composition, wherein the high-value materials include at least one of magnesium carbonate, calcium carbonate, potash, phosphate, heavy metals, and/or a combination thereof.\|[0014] In some embodiments, the carbonate-enhanced nutrition composition is used as fertilizer in agriculture and/or as M-sand in the construction field.\|[0015] . In some embodiments, the refill docking platform includes a connection part that is configured to hold the refill cartridge in an invertedly upright position to enable the flow of the substance from the refill cartridge to the bottom of the primary compartment.\|[0016] The method of preparing a carbonate-enhanced nutrition composition of the present description includes a more direct approach for capturing and storing carbon dioxide from the atmosphere using the geo-bag. The direct approach represents the geo-bag that includes a simple configuration used in an outdoor environment for capturing and storing carbon dioxide from the atmosphere. Such a simple configuration of geo-bag eliminates the need for a complicated arrangement of the carbon dioxide sequestration system used in the existing system.\|The geo-bag includes improved measurement, reporting, and verification (MRV) by enclosing the first mixture in a high surface area to volume ratio and staking in vertical layers to hold the first mixture, and the geo-bag acts as a structural member to produce a carbonate enhanced nutrition composition at a lower economical level. Such carbonate-enhanced nutrition composition includes high economic value materials, which can be used as a fertilizer for agricultural fields or building construction material, e.g. M-sand.\|[0017] These and other aspects of the embodiments herein will be better appreciated and understood when considered in conjunction with the following description and the accompanying drawings. It should be understood, however, that the following descriptions, while indicating preferred embodiments and numerous specific details thereof, are given by way of illustration and not of limitation. Many changes and modifications may be made within the scope of the embodiments herein without departing from the spirit thereof, and the embodiments herein include all such modifications.\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] The embodiments herein will be better understood from the following detailed description with reference to the drawings, in which:\|[0019] FIG. 1 is a block diagram that illustrates a systemforpreparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein;\|[0020] FIG. 2 illustrates a process of preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein;\|[0021] FIGS. 3A- 3Bareflow diagrams that illustratea method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein; and\|[0022] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence\|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS. 3A-3B of the present disclosure according to some embodiments herein.\|DETAILED\|DESCRIPTION OF PREFERRED EMBODIMENTS\|[0023] The embodiments herein and the various features and advantageous details thereof are explained more fully with reference to the non-limiting embodiments that are illustrated in the accompanying drawings and detailed in the following description. Descriptions of well-known components and processing techniques are omitted so as to not unnecessarily obscure the embodiments herein. The examples used herein are intended merely to facilitate an understanding of ways in which the embodiments herein may be practiced and to further enable those of skill in the art to practice the embodiments herein. Accordingly, the examples should not be construed as limiting the scope of the embodiments herein.\|[0024] In the view of the foregoing, the need for a system and methodfor producing carbonate-enhanced nutrition composition using a geo-bag is in the ongoing description.\|Referring now to the drawings, and more particularly to FIGS. 1 through 4D, where similar reference characters denote corresponding features in a consistent manner throughout the figures, there are shown preferred embodiments.\|[0025] FIG. 1 is a block diagram that illustrates a system 100for preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. The system 100 includesa rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The rock crushing unit 102 receives rocks from a source station for compressing and breaking the rocks into small particles. In some embodiments, the source station may be a quarry or a mining area, and the rock is extracted using explosives or mechanical excavators to remove the rock from the ground. The rock crushing unit 102 may include an input unit, a series of crushing and screening units, a transporting unit, and a storage area. The input unit may include a hopper for feeding the rocks and is passed through the series of crushing and screening units for compressing and breaking the rocks into desiredsizes to obtain crushed rocks. The crushed rocks are forwarded to the transporting unit. The transporting unit may include a conveyor belt that carries the crushed rocks to the storage area or an end location. In some embodiments, the crushing and screening unit includes but is not limited to a jaw crusher, a cone crusher, an impact crusher, a gyratory crusher, a ball mill crusher, a feeder breaker, a roll crusher, or a combination thereof.\|[0026] The reactor 108 is connected to the rock crushing unit 102 for receiving the smaller particles of crushed rocks. The urban organic wastage collection unit 104 receives municipal waste and is connected to the organic acid extraction unit 106 to produce organic acidcomponents through an electro-microbial process (EMP). The urban organic wastage collection unit 104 collects and stores organic waste, including municipal solid waste, industrial organic wastes, and or agricultural wastes to produce a biomass material. The biomass material may be produced using a microbial technique.\|[0027] The reactor 108 is connected to the organic acid extraction unit 106 to mix the organic acid componentthat is extracted from a biomass materialwith the crushed rocks to prepare a carbon-sequestration substrate. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere. In some embodiments, the organic acid component is extracted by a liquefaction reaction of biomass under supercritical conditions. The liquefaction reaction of biomass under supercritical conditions results in an effective decomposition of biomass. The supercritical condition may include the addition of water to the biomass and increasing its temperature above the boiling point of the water at which the water has a high pressure and high concentration of H+ and OH- ions. Such supercritical conditions help the conversion of liquefied biomass into cellulose-derived monosaccharides. The cellulosederived monosaccharide is degraded into some short-chain intermediates in the absence of oxidant to produce value-added chemicals that includethe organic acid components. The organic acid components may include but are not limited to acetic acid, citric acid, 2,5-diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid or 2,5-furandicarboxylic acid (FDCA).\|[0028] The reactor 108 is configured for mixing about 70% to 90% of weight/weight\|(w/w) of the crushed rocks and about 10% to 30% weight/volume (w/V) of the organic acid components to prepare a carbon-sequestration substrate at a predetermined mixing condition.\|The predetermined mixing condition may include a mixing temperature ranging from 25°C to\|30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over 2 hours - 48 hours to prepare thecarbon-sequestration substrate.\|[0029] The geo-bag 112 receives the carbon-sequestration substrate from the reactor 108\|through a spray head. The carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and has a pH value ranging from 2.5 to 3.5.\|[0030] The conveyor unit 110 is configured for carrying the carbon-sequestration substrate to a filling station from the reactor 108. The filling station is provided with the geo-bag\|112. In some embodiments, the geo-bag 112 is made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 112. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE),or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3 millimeters (mm). The geo-bag 112 is made from eco-friendly materials that do not decompose over the rock carbonation period, allow selective exchange of material between the bag contents and the environment, and allow retrieval of crushed rock post the carbonation period.\|[0031] The geo-bag 112 is filled with the carbon-sequestration substrate to prepare a carbon-sequestration package. In some embodiments, the geo-bag 112 is filled by dispensing the carbon-sequestration substratethrough a sand spray head that is arranged in the reactor 108. The dispensation of the carbon-sequestration substrateis controlled from the reactor 108 in the thickness of 1 cm to 12 inches at rates of 40-200 tons/hr.\|[0032] The carbon-sequestration packages are transferred to an operating location using a transportation medium. The transportation medium may be a conveyor belt, truck, or manual process.\|[0033] The carbon-sequestration packages are allowed for a rock carbonation period in the operating location by stacking or burying the packages in the operating location. The rock carbonation period may be 2-5 years. The carbon-sequestration substratein a package is enabled to capture the carbon dioxide from the atmosphere and convert thecarbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Thereby, the concentration level of\|CO2 in the atmosphere is reduced. The carbonate-enhanced nutrition compositionincludes high economic value materials, including but not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0034] FIG. 2 illustrates a process 200 for preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein. The process 200 includes a stone crusher 202, a sand grinding ball mill 204, a conveyor unit 206, and a geo-bag 208. The stone crusher 202includes a series of cone crushing units and an automatic feeding arrangement for receiving rock from a source station (e.g.mining area or quarry)for compressing and breaking the rocks into small particles to obtain crushed rocks. The sand grinding ball mill 204 receives the crushed rocks from thestone crusher 202 and mixes the crushed rocks with an organic acid component at a predetermined mixing condition to prepare a carbon-sequestration substrate. The organic acid component is extracted from biomass using an organic acid extraction unit. The conveyor unit 206 carries the carbon-sequestration substrateto a filling station from the sand grinding ball mill 204. The filling station is provided withthe geo-bag 208, whichis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 208. The geo-bag 208 is filled with the carbon-sequestration substrateto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportationmedium. The packages are stacked or buried fora rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere resulting in the conversion of the carbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Such carbonate-enhanced nutrition composition includes high economic value materials including but not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0035] FIGS. 3A-3B are flow diagrams that illustrate a method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. At step\|302, the method includes receiving the rocks from the ground and preparing the crushed rocks by compressing and breaking the rocks into small particles using the rock crushing unit. The crushed rocks include a particle size below 5 mm.\|[0036] At step 304, the method includes collecting and storing organic wastes using the urban organic waste collection unit to produce biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof. The biomass material may be produced using a microbial technique.\|[0037] At step 306, the method includes extracting an organic acid component from the biomass using the organic acid extraction unit. The organic acid component may be extracted using an electro-microbial production (EMP) technique. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketogluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-\|Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere.\|[0038] At step 308, the method includes mixing the crushed rocks in a concentration ranging from 70% to 90% of weight/weight (w/w) and the organic acid component in a concentration ranging from 10% to 30% weight/volume (w/V) to prepare a carbon-sequestration substrate at a predetermined mixing condition using the reactor. The predetermined mixing condition may include a mixing temperature ranging from 25°C to 30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over a few hours to a few days of the period to prepare the carbon-sequestration substrate. In some embodiments, the carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and pH value ranging from 2.5 to 3.5.\|[0039] At step 310, the method includes preparing the geo-bagusing an eco-friendly material that allows selective exchange of material between the bag contents and the environment. The geo-bag does not decompose over the rock carbonation period and allows retrieval of a carbonate-enhanced nutrition composition during the carbonation period. The geo20\|bagis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE), or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3\|millimeters (mm).\|[0040] At step 312, the method includes filling the carbon-sequestration substrate, using a sand spray head arranged in the reactor, into the geo-bagto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportation medium.\|The transportation medium may be a conveyor belt, a truck, or a manual process.\|[0041] At step 314, the method includes allowing the carbon-sequestration packages at a rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere. The packages are stacked or buried in the operating location at the rock carbonation period to capture the carbon dioxide from the atmosphere, resulting in the conversion of the carbon-sequestration substrate into a carbonate-enhanced nutrition composition, thereby reducing environmental CO2 level in the atmosphere. The rock carbonation period may include\|2-5 years. In some embodiments, the operating location is a forming land, construction site, or any other outdoor environment. The carbonate-enhanced nutrition composition is further processed to extract high economic value materials, including but are not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0042] TABLE 1 illustrates an approximate concentration level of high-value materials present in the carbonate-enhanced nutrition composition prepared using the method as described in FIG. 3 of the proposed disclosure.\|[0043] TABLE 1:\|Material Concentration level in percentage\|Potassium (K2O) 0.2 %\|Phosphate (P2O5) 0.4%\|Chromium 0.7%\|Nickel 0.7%\|CaCO3 4%\|[0044] TABLE 2 illustrates experimental results validating the efficiency of the carbonate-enhanced nutrition composition prepared using the method described in FIG. 3 of the present disclosure. The experiments are conducted to accelerate carbonation within a controlled environment, optimizing specific parameters to enhance carbon sequestration efficiency. The study evaluates carbonation performance under varying pH levels and particle sizes to identify the most effective conditions for CO₂ mineralization.\|[0045] TABLE 2:\|Samples\|Carbonization efficiency (%)\|Experiment A\|pH - 2.5 to 3.5\|Rock Size - < 5 mm\|Experiment B\|pH - 6.0 to 6.5\|rock - < 300 microns\|Dunite 60.77 22.7\|Basalt 14.33 7.5\|[0046] The above tabulation shows the experimental setup includes two different conditions: Experiment A is conducted at a pH range of 2.5 to 3.5 with crushed rock samples of less than 5 mm, while Experiment B is conducted at a pH range of 6.0 to 6.5 with a finer particle size of less than 300 microns. The process is carried out within a temperature range of 25°C to\|30°C, in a background bath of acetic acid, ensuring an optimized environment for carbonation.\|[0047] The results demonstrated significant differences in carbonation efficiency between the two experimental setups. Dunite samples exhibited a carbonation efficiency of\|60.77% in Experiment A (pH 2.5 to 3.5, rock size <5 mm), and the efficiency dropped to 22.7%\|in Experiment B (pH 6.0 to 6.5, rock size<300 microns). Similarly, basalt samples showed a carbonation efficiency of 14.33% in Experiment A, which reduced to 7.5% in Experiment B. The experimental results demonstrate that lower pH values and larger particle sizes enhanced carbonation particularly at the optimized conditions including pH 2.5 to 3.5 and the rock size is\|<5 mm.\|[0048] The experiment resultsdemonstrate that the carbonation efficiency is increased 15\|to 130 times higher thanthe natural carbonation process with the optimized conditions, including pH value ranging from 2.5 to 3.5 and the rock Size, includes less than 5 mm. These results validate the technical feasibility and efficiency gains of the method described in FIG. 3 of the proposed disclosure, confirming that the integration of crushed ultramafic and basaltic rocks, organic acid-based substrates, and a controlled carbonation process significantly enhances CO₂\|capture and mineralization efficiency.\|[0049] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence\|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3Bof the present disclosure according to some embodiments herein. The analysis shows the elemental compositions of dunite and basalt samples before and after carbonization process. FIGS. 4A - 4B are graphical representations illustrating the X-ray fluorescence (XRF) analysis of dunite rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the duniterock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw dunite rock samples; (iv) A - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out at the optimized condition including pH 2.5 to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5\|and the rock size including <300 microns. The results indicate that dunite samples subjected to carbonization under optimized conditions (pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw dunite samples and those carbonized under non-optimized conditions (pH 6.0-6.5, rock size <300 microns).\|[0050] FIGS. 4C - 4D are graphical representations illustrating the X-ray fluorescence\|(XRF) analysis of basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the basalt rock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw basalt rock samples; (iv) A - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out at the optimized condition including pH 2.5\|to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5 and the rock size including <300 microns.\|The results indicate that basalt samples subjected to carbonization under optimized conditions\|(pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw basalt samples and those carbonized under non-optimized conditions (pH 6.0-\|6.5, rock size <300 microns). The higher retention and conversion efficiency of valuable elements under optimized carbonation conditions confirm that the process facilitates effective mineralization and enhances sequestration efficiency.\|[0051] The foregoing description of the specific embodiments will so fully reveal the general nature of the embodiments herein that others can, by applying current knowledge, readily modify and/or adapt for various applications such specific embodiments without departing from the generic concept, and, therefore, such adaptations and modifications should and are intended to be comprehended within the meaning and range of equivalents of the disclosed embodiments.\|It is to be understood that the phraseology or terminology employed herein is for the purpose of description and not of limitation. Therefore, while the embodiments herein have been described in terms of preferred embodiments, those skilled in the art will recognize that the embodiments herein can be practiced with modification within the spirit and scope.	(IN202441017388)\|Technical Field\|[0001] The embodiments herein generally relate toa carbon mineralization method, and more particularly, a system and method for preparing carbonate-enhanced nutrition composition using a geo-bag. Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.\|Description of the Related Art\|[0002] In recent years, the significantriseinatmospheric carbon dioxide (CO2) levels has been identified as a leading cause of climate change on Earth. To mitigate this issue, carbon mineralization, or carbon sequestration, has emerged as a prominent method. Carbon mineralization is a process of converting carbon dioxide into solid minerals, such as carbonate, through a chemical reaction. This reaction occurs when specific types of rocks, such as serpentine, basalt, mafic, ultramafic, etc., are exposed to carbon dioxide, resulting in the formation of carbonate-enhanced minerals. Hence, the atmospheric CO2 level is stabilized asthe reacted carbon remains bound within the solid minerals, preventing its release into the atmosphere. However, it is important to note that this process typically requires several years to effectively reduce carbon levels in the atmosphere.\|[0003] Most of the existing carbon sequestration systemsto produce carbonate-enhanced mineralsutilize indoor techniques, employingan indirect method. For example, thesesystemsincludea mineral dissolution reactor for mixing various materials. These materials include magnesium or calcium, which is available in the rocks (e.g. serpentine, olivine, basalt, or labradorite), organic acid, and chelating agents. Through this mixing process, a magnesium or calcium-rich solvent is synthesized tocapture and store carbon dioxide. Additionally, these existing systemsinclude a combined biocatalyst and carbonation reactor, along witha control module for expediting the process of sequestration of carbon. However, the current indoor technique requires a more complicated arrangement and entails higher costs.\|[0004] Accordingly, there remains a need for a more simple and direct approach to capture and store the carbon dioxide from the atmosphere at a reduced economic level and to produce a carbonated enhanced nutrition composition using a geo-bag.\|SUMMARY\|[0005] In view of a foregoing, an embodiment herein provides a method for preparing a carbonate-enhanced nutrition composition using a geo-bag. The method includes i) collecting and crushing rocks into small particles, using a rock crushing unit; ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbonsequestration substrate using a reactor by mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions. The carbon-sequestration substrate is filled into geo-bags to prepare carbon-sequestration packages. The geo-bag includes an eco-friendly material that only permits water and air to pass through while retaining the substrate. The geo-bag consists of a thickness ranging from 50 microns to 3 millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbon-sequestration substrate by subjecting the carbonsequestration packages to a rock-carbonation period at an operating location to capture atmospheric carbon dioxide. The geo-bag acts as a structural member providing a high surface area-to-volume ratio to optimize carbon dioxide capture resulting in 15 to 130 times enhanced carbonation efficiency.\|[0006] In some embodiments, the crushed rocks include at least one of olivine, dunite, ultramafic, basalt, serpentine, and/or a combination thereof. The crushed rocks include a particle size below 5 mm.\|[0007] In some embodiments, the predefined mixing conditions include a mixing temperature ranging from 25°C to 30°C and an atmospheric pressure ranging from 1 atm to 2\|atm.\|[0008] In some embodiments, the carbon-sequestration substrate includes a concentration level ranging from 400 parts per million (ppm) to 450 ppm, a moisture content ranging from\|25% to 95% of rock weight and a pH value ranging from 2.5 to 3.5.\|[0009] In some embodiments, the geo-bag includes at least one of the geotextiles, highdensity polyethylene (HDPE), and/or a combination thereof.\|[0010] In some embodiments, the rock-carbonation period ranges from 2 years to 5 years.\|[0011] In some embodiments, the organic acid component is extracted using an electromicrobial production (EMP) technique from the biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof.\|[0012] In some embodiments, the operating location includes at least one farming land, a construction site, and an outdoor environment.\|[0013] In some embodiments, the method includes extracting high-value materials from the carbonate-enhanced nutrition composition, wherein the high-value materials include at least one of magnesium carbonate, calcium carbonate, potash, phosphate, heavy metals, and/or a combination thereof.\|[0014] In some embodiments, the carbonate-enhanced nutrition composition is used as fertilizer in agriculture and/or as M-sand in the construction field.\|[0015] . In some embodiments, the refill docking platform includes a connection part that is configured to hold the refill cartridge in an invertedly upright position to enable the flow of the substance from the refill cartridge to the bottom of the primary compartment.\|[0016] The method of preparing a carbonate-enhanced nutrition composition of the present description includes a more direct approach for capturing and storing carbon dioxide from the atmosphere using the geo-bag. The direct approach represents the geo-bag that includes a simple configuration used in an outdoor environment for capturing and storing carbon dioxide from the atmosphere. Such a simple configuration of geo-bag eliminates the need for a complicated arrangement of the carbon dioxide sequestration system used in the existing system.\|The geo-bag includes improved measurement, reporting, and verification (MRV) by enclosing the first mixture in a high surface area to volume ratio and staking in vertical layers to hold the first mixture, and the geo-bag acts as a structural member to produce a carbonate enhanced nutrition composition at a lower economical level. Such carbonate-enhanced nutrition composition includes high economic value materials, which can be used as a fertilizer for agricultural fields or building construction material, e.g. M-sand.\|[0017] These and other aspects of the embodiments herein will be better appreciated and understood when considered in conjunction with the following description and the accompanying drawings. It should be understood, however, that the following descriptions, while indicating preferred embodiments and numerous specific details thereof, are given by way of illustration and not of limitation. Many changes and modifications may be made within the scope of the embodiments herein without departing from the spirit thereof, and the embodiments herein include all such modifications.\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] The embodiments herein will be better understood from the following detailed description with reference to the drawings, in which:\|[0019] FIG. 1 is a block diagram that illustrates a systemforpreparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein;\|[0020] FIG. 2 illustrates a process of preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein;\|[0021] FIGS. 3A- 3Bareflow diagrams that illustratea method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein; and\|[0022] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence\|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS. 3A-3B of the present disclosure according to some embodiments herein.\|DETAILED\|DESCRIPTION OF PREFERRED EMBODIMENTS\|[0023] The embodiments herein and the various features and advantageous details thereof are explained more fully with reference to the non-limiting embodiments that are illustrated in the accompanying drawings and detailed in the following description. Descriptions of well-known components and processing techniques are omitted so as to not unnecessarily obscure the embodiments herein. The examples used herein are intended merely to facilitate an understanding of ways in which the embodiments herein may be practiced and to further enable those of skill in the art to practice the embodiments herein. Accordingly, the examples should not be construed as limiting the scope of the embodiments herein.\|[0024] In the view of the foregoing, the need for a system and methodfor producing carbonate-enhanced nutrition composition using a geo-bag is in the ongoing description.\|Referring now to the drawings, and more particularly to FIGS. 1 through 4D, where similar reference characters denote corresponding features in a consistent manner throughout the figures, there are shown preferred embodiments.\|[0025] FIG. 1 is a block diagram that illustrates a system 100for preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. The system 100 includesa rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The rock crushing unit 102 receives rocks from a source station for compressing and breaking the rocks into small particles. In some embodiments, the source station may be a quarry or a mining area, and the rock is extracted using explosives or mechanical excavators to remove the rock from the ground. The rock crushing unit 102 may include an input unit, a series of crushing and screening units, a transporting unit, and a storage area. The input unit may include a hopper for feeding the rocks and is passed through the series of crushing and screening units for compressing and breaking the rocks into desiredsizes to obtain crushed rocks. The crushed rocks are forwarded to the transporting unit. The transporting unit may include a conveyor belt that carries the crushed rocks to the storage area or an end location. In some embodiments, the crushing and screening unit includes but is not limited to a jaw crusher, a cone crusher, an impact crusher, a gyratory crusher, a ball mill crusher, a feeder breaker, a roll crusher, or a combination thereof.\|[0026] The reactor 108 is connected to the rock crushing unit 102 for receiving the smaller particles of crushed rocks. The urban organic wastage collection unit 104 receives municipal waste and is connected to the organic acid extraction unit 106 to produce organic acidcomponents through an electro-microbial process (EMP). The urban organic wastage collection unit 104 collects and stores organic waste, including municipal solid waste, industrial organic wastes, and or agricultural wastes to produce a biomass material. The biomass material may be produced using a microbial technique.\|[0027] The reactor 108 is connected to the organic acid extraction unit 106 to mix the organic acid componentthat is extracted from a biomass materialwith the crushed rocks to prepare a carbon-sequestration substrate. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere. In some embodiments, the organic acid component is extracted by a liquefaction reaction of biomass under supercritical conditions. The liquefaction reaction of biomass under supercritical conditions results in an effective decomposition of biomass. The supercritical condition may include the addition of water to the biomass and increasing its temperature above the boiling point of the water at which the water has a high pressure and high concentration of H+ and OH- ions. Such supercritical conditions help the conversion of liquefied biomass into cellulose-derived monosaccharides. The cellulosederived monosaccharide is degraded into some short-chain intermediates in the absence of oxidant to produce value-added chemicals that includethe organic acid components. The organic acid components may include but are not limited to acetic acid, citric acid, 2,5-diketo-gluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid or 2,5-furandicarboxylic acid (FDCA).\|[0028] The reactor 108 is configured for mixing about 70% to 90% of weight/weight\|(w/w) of the crushed rocks and about 10% to 30% weight/volume (w/V) of the organic acid components to prepare a carbon-sequestration substrate at a predetermined mixing condition.\|The predetermined mixing condition may include a mixing temperature ranging from 25°C to\|30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over 2 hours - 48 hours to prepare thecarbon-sequestration substrate.\|[0029] The geo-bag 112 receives the carbon-sequestration substrate from the reactor 108\|through a spray head. The carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and has a pH value ranging from 2.5 to 3.5.\|[0030] The conveyor unit 110 is configured for carrying the carbon-sequestration substrate to a filling station from the reactor 108. The filling station is provided with the geo-bag\|112. In some embodiments, the geo-bag 112 is made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 112. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE),or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3 millimeters (mm). The geo-bag 112 is made from eco-friendly materials that do not decompose over the rock carbonation period, allow selective exchange of material between the bag contents and the environment, and allow retrieval of crushed rock post the carbonation period.\|[0031] The geo-bag 112 is filled with the carbon-sequestration substrate to prepare a carbon-sequestration package. In some embodiments, the geo-bag 112 is filled by dispensing the carbon-sequestration substratethrough a sand spray head that is arranged in the reactor 108. The dispensation of the carbon-sequestration substrateis controlled from the reactor 108 in the thickness of 1 cm to 12 inches at rates of 40-200 tons/hr.\|[0032] The carbon-sequestration packages are transferred to an operating location using a transportation medium. The transportation medium may be a conveyor belt, truck, or manual process.\|[0033] The carbon-sequestration packages are allowed for a rock carbonation period in the operating location by stacking or burying the packages in the operating location. The rock carbonation period may be 2-5 years. The carbon-sequestration substratein a package is enabled to capture the carbon dioxide from the atmosphere and convert thecarbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Thereby, the concentration level of\|CO2 in the atmosphere is reduced. The carbonate-enhanced nutrition compositionincludes high economic value materials, including but not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0034] FIG. 2 illustrates a process 200 for preparing a carbonate-enhanced nutrition composition using a geo-bag according to some embodiments herein. The process 200 includes a stone crusher 202, a sand grinding ball mill 204, a conveyor unit 206, and a geo-bag 208. The stone crusher 202includes a series of cone crushing units and an automatic feeding arrangement for receiving rock from a source station (e.g.mining area or quarry)for compressing and breaking the rocks into small particles to obtain crushed rocks. The sand grinding ball mill 204 receives the crushed rocks from thestone crusher 202 and mixes the crushed rocks with an organic acid component at a predetermined mixing condition to prepare a carbon-sequestration substrate. The organic acid component is extracted from biomass using an organic acid extraction unit. The conveyor unit 206 carries the carbon-sequestration substrateto a filling station from the sand grinding ball mill 204. The filling station is provided withthe geo-bag 208, whichis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag 208. The geo-bag 208 is filled with the carbon-sequestration substrateto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportationmedium. The packages are stacked or buried fora rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere resulting in the conversion of the carbon-sequestration substrateinto a carbonate-enhanced nutrition composition. Such carbonate-enhanced nutrition composition includes high economic value materials including but not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0035] FIGS. 3A-3B are flow diagrams that illustrate a method of preparing a carbonateenhanced nutrition composition using a geo-bag according to some embodiments herein. At step\|302, the method includes receiving the rocks from the ground and preparing the crushed rocks by compressing and breaking the rocks into small particles using the rock crushing unit. The crushed rocks include a particle size below 5 mm.\|[0036] At step 304, the method includes collecting and storing organic wastes using the urban organic waste collection unit to produce biomass. The biomass is generated from the decomposition of at least one of the organic municipal wastes, microalgae, industrial organic wastes, agricultural wastes, and/or a combination thereof. The biomass material may be produced using a microbial technique.\|[0037] At step 306, the method includes extracting an organic acid component from the biomass using the organic acid extraction unit. The organic acid component may be extracted using an electro-microbial production (EMP) technique. The organic acid component may be selected from the group consisting of but not limited to acetic acid, citric acid, 2,5- diketogluconic acid, gluconic acid, levulinic acid, furfural acid, lactic acid, formic acid, or 2,5-\|Furandicarboxylic acid (FDCA) or a combination thereof. In some embodiments, the organic acid component is Gluconic acid, which is non-toxic and mild, is used to accelerate the weathering or mineralization process of rocks by capturing CO2 from the atmosphere.\|[0038] At step 308, the method includes mixing the crushed rocks in a concentration ranging from 70% to 90% of weight/weight (w/w) and the organic acid component in a concentration ranging from 10% to 30% weight/volume (w/V) to prepare a carbon-sequestration substrate at a predetermined mixing condition using the reactor. The predetermined mixing condition may include a mixing temperature ranging from 25°C to 30°C, an atmospheric pressure ranging from 1 atm to 2 atm, and a concentration level of the carbon-sequestration substrate ranging from 400 part per million (ppm) to 450 ppm. The mixing process is carried out continuously over a few hours to a few days of the period to prepare the carbon-sequestration substrate. In some embodiments, the carbon-sequestration substrate includes the moisture content ranging from 25% to 95% of rock weight and pH value ranging from 2.5 to 3.5.\|[0039] At step 310, the method includes preparing the geo-bagusing an eco-friendly material that allows selective exchange of material between the bag contents and the environment. The geo-bag does not decompose over the rock carbonation period and allows retrieval of a carbonate-enhanced nutrition composition during the carbonation period. The geo20\|bagis made up of a material such that the bag allows only water and air to pass through while trapping the component inside the geo-bag. The material may be selected from the group consisting of but not limited to geotextiles, high-density polyethylene (HPDE), or other such materials. The geo-bag 112 can be fabricated with specific thicknesses, fiber density, and specific raw materials. The geo-bag 112 includes a thickness ranging from 50 microns to 3\|millimeters (mm).\|[0040] At step 312, the method includes filling the carbon-sequestration substrate, using a sand spray head arranged in the reactor, into the geo-bagto prepare a carbon-sequestration package. The packages are transported to an operating location using a transportation medium.\|The transportation medium may be a conveyor belt, a truck, or a manual process.\|[0041] At step 314, the method includes allowing the carbon-sequestration packages at a rock carbonation period in the operating location to capture the carbon dioxide from the atmosphere. The packages are stacked or buried in the operating location at the rock carbonation period to capture the carbon dioxide from the atmosphere, resulting in the conversion of the carbon-sequestration substrate into a carbonate-enhanced nutrition composition, thereby reducing environmental CO2 level in the atmosphere. The rock carbonation period may include\|2-5 years. In some embodiments, the operating location is a forming land, construction site, or any other outdoor environment. The carbonate-enhanced nutrition composition is further processed to extract high economic value materials, including but are not limited to calcium carbonate, potash, phosphate, and heavy metals.\|[0042] TABLE 1 illustrates an approximate concentration level of high-value materials present in the carbonate-enhanced nutrition composition prepared using the method as described in FIG. 3 of the proposed disclosure.\|[0043] TABLE 1:\|Material Concentration level in percentage\|Potassium (K2O) 0.2 %\|Phosphate (P2O5) 0.4%\|Chromium 0.7%\|Nickel 0.7%\|CaCO3 4%\|[0044] TABLE 2 illustrates experimental results validating the efficiency of the carbonate-enhanced nutrition composition prepared using the method described in FIG. 3 of the present disclosure. The experiments are conducted to accelerate carbonation within a controlled environment, optimizing specific parameters to enhance carbon sequestration efficiency. The study evaluates carbonation performance under varying pH levels and particle sizes to identify the most effective conditions for CO₂ mineralization.\|[0045] TABLE 2:\|Samples\|Carbonization efficiency (%)\|Experiment A\|pH - 2.5 to 3.5\|Rock Size - < 5 mm\|Experiment B\|pH - 6.0 to 6.5\|rock - < 300 microns\|Dunite 60.77 22.7\|Basalt 14.33 7.5\|[0046] The above tabulation shows the experimental setup includes two different conditions: Experiment A is conducted at a pH range of 2.5 to 3.5 with crushed rock samples of less than 5 mm, while Experiment B is conducted at a pH range of 6.0 to 6.5 with a finer particle size of less than 300 microns. The process is carried out within a temperature range of 25°C to\|30°C, in a background bath of acetic acid, ensuring an optimized environment for carbonation.\|[0047] The results demonstrated significant differences in carbonation efficiency between the two experimental setups. Dunite samples exhibited a carbonation efficiency of\|60.77% in Experiment A (pH 2.5 to 3.5, rock size <5 mm), and the efficiency dropped to 22.7%\|in Experiment B (pH 6.0 to 6.5, rock size<300 microns). Similarly, basalt samples showed a carbonation efficiency of 14.33% in Experiment A, which reduced to 7.5% in Experiment B. The experimental results demonstrate that lower pH values and larger particle sizes enhanced carbonation particularly at the optimized conditions including pH 2.5 to 3.5 and the rock size is\|<5 mm.\|[0048] The experiment resultsdemonstrate that the carbonation efficiency is increased 15\|to 130 times higher thanthe natural carbonation process with the optimized conditions, including pH value ranging from 2.5 to 3.5 and the rock Size, includes less than 5 mm. These results validate the technical feasibility and efficiency gains of the method described in FIG. 3 of the proposed disclosure, confirming that the integration of crushed ultramafic and basaltic rocks, organic acid-based substrates, and a controlled carbonation process significantly enhances CO₂\|capture and mineralization efficiency.\|[0049] FIGS. 4A - 4D are graphical representations that illustrate an X-ray fluorescence\|(XRF) analysis of dunite and basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3Bof the present disclosure according to some embodiments herein. The analysis shows the elemental compositions of dunite and basalt samples before and after carbonization process. FIGS. 4A - 4B are graphical representations illustrating the X-ray fluorescence (XRF) analysis of dunite rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the duniterock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw dunite rock samples; (iv) A - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out at the optimized condition including pH 2.5 to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the dunite rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5\|and the rock size including <300 microns. The results indicate that dunite samples subjected to carbonization under optimized conditions (pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw dunite samples and those carbonized under non-optimized conditions (pH 6.0-6.5, rock size <300 microns).\|[0050] FIGS. 4C - 4D are graphical representations illustrating the X-ray fluorescence\|(XRF) analysis of basalt rock samples before and after carbonization process carried out using the method as described in FIGS.3A-3B of the present disclosure. In the graph: (i) x-axis represents the high valued materials present in the basalt rock samples; (ii) the y-axis represents concentration of materials before and after before and after carbonization process; (iii) R - represents the concentration level of high valued materials present in the raw basalt rock samples; (iv) A - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out at the optimized condition including pH 2.5\|to 3.5 and the rock size is <5 mm; and (v) B - represents the concentration level of high valued materials present in the basalt rock samples after carbonization process carried out under the condition including pH value ranging from 6.0 to 6.5 and the rock size including <300 microns.\|The results indicate that basalt samples subjected to carbonization under optimized conditions\|(pH 2.5-3.5, rock size <5 mm) exhibit an enhanced concentration of high-value materials compared to raw basalt samples and those carbonized under non-optimized conditions (pH 6.0-\|6.5, rock size <300 microns). The higher retention and conversion efficiency of valuable elements under optimized carbonation conditions confirm that the process facilitates effective mineralization and enhances sequestration efficiency.\|[0051] The foregoing description of the specific embodiments will so fully reveal the general nature of the embodiments herein that others can, by applying current knowledge, readily modify and/or adapt for various applications such specific embodiments without departing from the generic concept, and, therefore, such adaptations and modifications should and are intended to be comprehended within the meaning and range of equivalents of the disclosed embodiments.\|It is to be understood that the phraseology or terminology employed herein is for the purpose of description and not of limitation. Therefore, while the embodiments herein have been described in terms of preferred embodiments, those skilled in the art will recognize that the embodiments herein can be practiced with modification within the spirit and scope.	Family Number\|(116031041)\|116031041\|Object of Invention\|(IN202441017388 A)\|Moreover, the present invention relates to a method of capturing and storing carbon dioxide from the atmosphereusing geo-bags.\|Abstract\|(IN202441017388 A)\|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112. The system includes a rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The reactor 108 mixes crushed rocks and organic acid components to prepare a carbon-sequestration substrate. The geo-bag 112 is filled with the carbon-sequestration substrate, and the geo-bag 112 is made from eco-friendly materials, allowing selective exchange of components between the bag contents and the environment. The substrate in the geo-bag 112 is allowed to capture the CO2 from the atmosphereand convert the carbon-sequestration substrate into a carbonateenhanced nutrition composition, thereby reducing the environmental CO2 level. The composition includes high economic value materials like calcium carbonate, potash, phosphate, and heavy metals. The composition can be used as a fertilizer or building construction material like M-sand.\|Independent Claims\|(IN202441017388 A)\|1. A method for preparing a carbonate-enhanced nutrition composition using a geo-bag (112) wherein the method comprising: i) Collecting and crushing rocks into small particles, using a rock crushing unit (102); ii) Extracting acetic acid compound from biomass, using an organic acid extraction unit; iii) Synthesizing a carbon-sequestration substrate, using a reactor (108) by Characterized in that, a) mixing 70% to 90% weight/weight (w/w) of the crushed rocks with 10% to 30% weight/volume (w/v) of the acetic acid compound under predefined mixing conditions; and b) filling the carbon-sequestration substrate into the geo-bag (112) to prepare carbon-sequestration packages, wherein the geo-bag (112) comprises an ecofriendly material that permits only water and air to pass through while (...) millimeters; iv) synthesizing a carbonate-enhanced nutrition composition from the carbonsequestration substrate by subjecting the carbon-sequestration packages to a rockcarbonation period at an operating location to capture atmospheric carbon dioxide; wherein the geo-bag (112) acts as a structural member providing a high surface area-tovolume ratio to optimize carbon dioxide capture resulting 15 to 130 times enhanced carbonation efficiency.\|	Other special machines				A01G-024/12\|A01G-024/15\|A01G-024/17\|A01G-024/20\|A01G-024/60	A01G-024/12\|A01G-024/15\|A01G-024/17\|A01G-024/20\|A01G-024/60										PENDING	(IN202441017388)\|PENDING	ALIVE	(IN202441017388)\|ALIVE	(IN202441017388)\|LEGAL DETAILS FOR IN202441017388\|Actual or expected expiration date=2044-03-11\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-11\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN202441017388\|Application date=2024-03-11\|Standardized application number=2024IN-41017388\|Event publication date=2025-09-12\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN202441017388\|Publication stage code=A\|Publication date=2025-09-12\|Standardized publication number=IN202441017388		(IN202441017388)\|IN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=/WizbbSQlgu/uP20qNF3JE9lJnxGv8IZa/WZFbsCsqzB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=IN0000000001670167&ekey=2476&xpn=IN202441017388&kind=A	https://iprsearch.ipindia.gov.in/PublicSearch/PublicationSearch/ApplicationStatus	https://permalink.orbit.com/RenderStaticFirstPage?XPN=dR15du4ks0vl9J154pQkJcExnvIz5kLrfqHome9U%252B8A%3D%26n%3D1&id=0&base=FAMPAT	IN						(IN202441017388)\|NAME=Tannirkulam Ajay\|NAME=Margankunte Naveen	(IN202441017388)\|4	1	1					(IN202441017388)\|Number of Claims: NCL=10\|		(IN202441017388)\|ENGLISH (ENG)	(IN202441017388)\|Patent	Titre: (IN202441017388)\|System and method for preparing carbonate-enhanced nutrition composition using geo-bags Résumé: (IN202441017388)\|A system 100 of preparing a carbonate-enhanced nutrition composition using a geo-bag 112. The system includes a rock crushing unit 102, an urban organic wastage collection unit 104, an organic acid extraction unit 106, a reactor 108, a conveyor unit 110, and a geo-bag 112. The reactor 108 mixes crushed rocks and organic acid components to prepare a carbon-sequestration substrate. The geo-bag 112 is filled with the carbon-sequestration substrate, and the geo-bag 112 is made from eco-friendly materials, allowing selective exchange of components between the bag contents and the environment. The substrate in the geo-bag 112 is allowed to capture the CO2 from the atmosphereand convert the carbon-sequestration substrate into a carbonateenhanced nutrition composition, thereby reducing the environmental CO2 level. The composition includes high economic value materials like calcium carbonate, potash, phosphate, and heavy metals. The composition can be used as a fertilizer or building construction material like M-sand.	10	Abstract	gpt-4o-mini	yes	The article describes a system for preparing a carbon-sequestration substrate that captures CO₂ and converts it into carbonates, aligning with the topic of enhanced weathering and carbon sequestration.
13	US63/569,558P\|US19/089,278	WOCA2025/050423\|US19/089,278	WO2025/199637\|US20250297409	116035972	WO2025/199637 A1 2025-10-02 [WO2025199637]\|US20250297409 A1 2025-09-25 [US20250297409]	2024-03-25\|2025-03-25	2025-03-25\|2025-03-25	2025-10-02\|2025-09-25		(US20250297409)\|2045-03-25\|(WO2025/199637)\|2027-09-25	(US20250297409)\|Carbon sequestration sand-based material for synthetic turf fields	(US20250297409)\|A synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.	TARKETT SPORTS	(US20250297409)\|Tarkett Sports Canada Inc. ([CA])\|(WO2025/199637)\|TARKETT SPORTS CANADA INC. ([CA])	SMOLETT JASON\|HABIB ERIC\|CHISAM CHRISTOPHER	(US20250297409)\|Smolett Jason\|Habib Eric\|Chisam Christopher	(WO2025/199637)\|YIP, Vincent ([CA])	(US20250297409)\|As will be appreciated, mesh may be defined as the number of openings in one square inch of a screen.\|Furthermore, it will be appreciated that by placing the carbon sequestration sand 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air.\|It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|	(US20250297409)\|1. A synthetic turf system comprising: a backing; turf fibers extended upward from the backing; one or more infill layers positioned above the backing, below a top portion of the turf fibers; wherein the one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|12. Infill for a synthetic turf system, the infill comprising: carbon sequestration sand including silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh; and organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|17. A method of preparing a synthetic turf system, the method comprising: dispersing carbon sequestration sand over a top portion of turf fibers, wherein the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|	(US20250297409)\|According to another aspect, infill for a synthetic turf system includes carbon sequestration sand.\|As used in this application, "or" is intended to mean an inclusive "or" rather than an exclusive "or".\|In accordance with varying embodiments discussed herein, there is provided an artificial turf system that utilizes a material derived from one or more types of carbon sequestration sands, including, for example and without limitation, wollastonite sand (general formula CaSiO_3), limestone, basalt, or the like.\|	(US20250297409)\|CARBON SEQUESTRATION(100,154)\|CARBON SEQUESTRATION SAND(100,44)\|SYNTHETIC TURF FIELD(100,4)\|SAND MATERIAL(100,3)\|CARBON SEQUESTRATION SAND MATERIAL(100,1)\|INFILL LAYER(91,53)\|TURF FIBER(82,33)\|SILICATE ROCK(82,15)\|ROCK REACTION(71,14)\|SYNTHETIC TURF(63,70)\|WOLLASTONITE SAND(52,1)\|BACKING(47,38)\|ULTRAMAFIC ROCK(47,15)\|ELASTOMER PARTICLE(45,4)\|THERMOPLASTIC PARTICLE(43,4)\|BASE ROCK LAYER(41,38)\|RAINWATER(40,24)\|LAYERED INSTALLATION(40,1)\|MESH SCREEN(36,6)\|DISPERSING CARBON SEQUESTRATION(35,2)\|RUBBER PARTICLE(34,4)\|RAIN WATER TRAVEL(32,1)\|BICARBONATE(30,10)\|COATED PARTICLE(30,4)\|ORGANIC PARTICLE(30,4)\|SYNTHETIC TURF BACKING(30,1)\|SYNTHETIC TURF INFILL LAYER(29,1)\|WEATHERED PARTICLE(28,2)\|INFILL(26,10)\|LIMESTONE(26,10)\|CARBON SEQUESTRATION LAYER(26,3)\|BASALT(25,8)\|SUBGRADE(23,9)\|TURF FIBER ANDTHE TOP(23,1)\|ARTIFICIAL TURF(22,2)\|PERIDOTITE(21,4)\|TURF(20,3)\|DUNITE(19,4)\|SPHERICITY(16,3)\|INFILL LAYER THICKNESS(16,2)\|POROSITY(13,2)\|GROUND(12,3)\|CARBONATE SEDIMENT(11,3)\|TURF CARPET(11,2)\|SHOCK PAD(10,6)\|CARBON SEQUESTRATION SAND INFILL(10,2)\|DRAINAGE STONE(10,2)\|OLIVINE(9,8)\|ROCK COMPACTION(9,2)\|HARDWOOD SAPWOOD(9,1)\|GEOTEXTILE COMPONENT(8,4)\|CONJOINED CLAUSE(8,1)\|SUBDRAIN TRENCH COMPONENT STONE(8,1)\|TURF FIBER STABILIZATION(8,1)\|CARBON DIOXIDE(7,10)\|PARTICLE SIZE(7,6)\|ARTIFICIAL GRASS BLADE(7,2)\|DRAINAGE PIPE(7,2)\|AERIAL SPREADER(7,1)\|ARTIFICIAL TURF INFILL(7,1)\|BALLAST INFILL(7,1)\|COMPACTION VARIABILITY(7,1)\|HANDHELD SPREADER(7,1)\|INFILL MIGRATION(7,1)\|LAYMOR BRUSH(7,1)\|PROPYLENE DIENE MONOMER(7,1)\|TURF BRUSHING EQUIPMENT(7,1)\|COMPACTED STONE BASE(6,2)\|DEACIDIFYING(6,2)\|HOPPER GATE(6,2)\|BROADCASTER TOOL(6,1)\|COCONUT PEAT(6,1)\|ENDPOINT RECITATION(6,1)\|OLIVE PIT(6,1)\|OSCILLATING BRUSH(6,1)\|PARTICLE SIZING(6,1)\|PERMEABLE BACKING(6,1)\|PNEUMATIC SPREADER(6,1)\|REGULAR DRAINAGE MEASURE(6,1)\|SEED TENDER(6,1)\|WALK BEHIND ROTARY BRUSH(6,1)\|CARBONIC ACID(5,6)\|MESH SIZE(5,4)\|CARBON SEQUESTRATION SAND LAYER(5,3)\|TRACTION(5,3)\|AIR BOOM SPREADER(5,1)\|BALL INTERACTION(5,1)\|HYDRAULIC BRUSH(5,1)\|INFILL LAYER REMAINDER(5,1)\|SYNTHETIC TURF ENVIRONMENTAL SUSTAINABILITY(5,1)\|TRIANGULAR BRUSH(5,1)\|COMPOSITIONAL RANGE(4,4)\|RIVER(4,4)\|SEA(4,4)\|BALLAST LAYER(4,2)\|BICARBONATE SOLUTION(4,2)\|DOLOMITE(4,2)\|DURABILITY(4,2)\|GRANITE(4,2)\|HYDRAULICALLY CONTROLLED CONVEYER(4,2)\|MINERAL NUTRIENT(4,2)\|STORM WATER(4,2)\|THERMOPLASTIC(4,2)\|BICARBONATE FORMATION(4,1)\|DESCRIPTOR(4,1)\|FLEXIBLE BRUSH(4,1)\|NATURAL GRASS BLADE(4,1)\|PACKING STABILITY(4,1)\|PARTICLE ETHYLENE(4,1)\|PUNCHED HOLE(4,1)\|RAIN WATER REACTION(4,1)\|RIGID BRUSH(4,1)\|ROTARY BRUSH ACTION(4,1)\|STRAIGHT BRUSH(4,1)\|SYNTHETIC TURF CAPACITY(4,1)\|SYNTHETIC TURF MANUFACTURING(4,1)\|STONE BASE LAYER(3,3)\|BAMBOO(3,1)\|CARBON CAPTURE BENEFIT(3,1)\|CARBON DIOXIDE DISSOLUTION(3,1)\|CARBONACEOUS MINERAL MATERIAL(3,1)\|CYPRESS(3,1)\|ELASTOMER(3,1)\|ENGINEERING(3,1)\|ENVIRONMENTALLY FRIENDLY(3,1)\|EQUILIBRIUM(3,1)\|EXHIBIT SUPERIOR MECHANICAL PERFORMANCE(3,1)\|GRAINING(3,1)\|GROOMER(3,1)\|HEARTWOOD(3,1)\|IDENTIFICATION(3,1)\|INFILL ARRANGEMENT(3,1)\|INFILL LAYER MINIMUM VOLUME(3,1)\|\|(WO2025/199637)\|CARBON SEQUESTRATION(100,154)\|SYNTHETIC TURF(100,71)\|CARBON SEQUESTRATION SAND(100,44)\|SAND MATERIAL(100,3)\|CARBON SEQUESTRATION SAND MATERIAL(100,1)\|SILICATE ROCK(88,15)\|INFILL LAYER(87,53)\|TURF FIBER(84,33)\|ROCK REACTION(77,14)\|DISPERSING CARBON SEQUESTRATION(55,2)\|ULTRAMAFIC ROCK(51,15)\|BACKING(45,38)\|RAINWATER(43,24)\|ELASTOMER PARTICLE(43,4)\|THERMOPLASTIC PARTICLE(42,4)\|BASE ROCK LAYER(39,38)\|LAYERED INSTALLATION(38,1)\|BICARBONATE(36,10)\|MESH SCREEN(34,6)\|INFILL(32,11)\|RUBBER PARTICLE(32,4)\|RAIN WATER TRAVEL(31,1)\|COATED PARTICLE(29,4)\|ORGANIC PARTICLE(29,4)\|SUBGRADE LAYER(29,1)\|SYNTHETIC TURF BACKING(29,1)\|SYNTHETIC TURF INFILL LAYER(28,1)\|WEATHERED PARTICLE(27,2)\|ENVIRONMENTALLY FRIENDLY(26,1)\|CARBON SEQUESTRATION LAYER(25,3)\|TRANSPORTATION(25,1)\|GEOTEXTILE(22,2)\|PERIDOTITE(20,4)\|TURF(19,3)\|LIMESTONE(18,10)\|DUNITE(18,4)\|BASALT(17,8)\|CARBON OFFSETTING(16,1)\|CARBON OFFSETTING INFILL MATERIAL(16,1)\|SPHERICITY(15,3)\|INFILL LAYER THICKNESS(15,2)\|POROSITY(13,2)\|CARBON NEUTRAL(13,1)\|INFILL MATERIAL(11,9)\|TURF CARPET(11,2)\|SHOCK PAD(10,6)\|CARBON SEQUESTRATION SAND INFILL(10,2)\|DRAINAGE STONE(10,2)\|HARDWOOD SAPWOOD(9,1)\|MECHANICAL RESISTANCE(9,1)\|OLIVINE(8,8)\|GEOTEXTILE COMPONENT(8,4)\|MECHANICAL PROPERTY(8,3)\|ROCK COMPACTION(8,2)\|CONJOINED CLAUSE(8,1)\|SUBDRAIN TRENCH COMPONENT STONE(8,1)\|TURF FIBER STABILIZATION(8,1)\|PARTICLE SIZE(7,6)\|ARTIFICIAL GRASS BLADE(7,2)\|DRAINAGE PIPE(7,2)\|AERIAL SPREADER(7,1)\|ARTIFICIAL TURF INFILL(7,1)\|BALLAST INFILL(7,1)\|COMPACTION VARIABILITY(7,1)\|HANDHELD SPREADER(7,1)\|INFILL MIGRATION(7,1)\|LAYMOR BRUSH(7,1)\|TURF BRUSHING EQUIPMENT(7,1)\|SEDIMENT(6,4)\|BROADCASTER TOOL(6,1)\|COCONUT PEAT(6,1)\|ENDPOINT RECITATION(6,1)\|OLIVE PIT(6,1)\|OSCILLATING BRUSH(6,1)\|PARTICLE SIZING(6,1)\|PERMEABLE BACKING(6,1)\|PNEUMATIC SPREADER(6,1)\|REGULAR DRAINAGE MEASURE(6,1)\|SEED TENDER(6,1)\|WALK BEHIND ROTARY BRUSH(6,1)\|WOLLASTONITE SAND(6,1)\|CARBONIC ACID(5,6)\|MESH SIZE(5,4)\|TRACTION(5,3)\|COMPACTED STONE BASE(5,2)\|DEACIDIFYING(5,2)\|HOPPER GATE(5,2)\|AIR BOOM SPREADER(5,1)\|BALL INTERACTION(5,1)\|COM COB(5,1)\|FORMULA CASIO(5,1)\|HIGH AVAILABILITY(5,1)\|HYDRAULIC BRUSH(5,1)\|INFILL LAYER REMAINDER(5,1)\|SYNTHETIC TURF ENVIRONMENTAL SUSTAINABILITY(5,1)\|TRIANGULAR BRUSH(5,1)\|COMPOSITIONAL RANGE(4,4)\|RIVER(4,4)\|SEA(4,4)\|BALLAST LAYER(4,2)\|BICARBONATE SOLUTION(4,2)\|CARBON SEQUESTRATION SAND LAYER(4,2)\|DOLOMITE(4,2)\|DURABILITY(4,2)\|GRANITE(4,2)\|HYDRAULICALLY CONTROLLED CONVEYER(4,2)\|MINERAL NUTRIENT(4,2)\|STORM WATER(4,2)\|THERMOPLASTIC(4,2)\|DESCRIPTOR(4,1)\|FLEXIBLE BRUSH(4,1)\|NATURAL GRASS BLADE(4,1)\|PACKING STABILITY(4,1)\|PUNCHED HOLE(4,1)\|RAIN WATER REACTION(4,1)\|RIGID BRUSH(4,1)\|ROTARY BRUSH ACTION(4,1)\|STRAIGHT BRUSH(4,1)\|SYNTHETIC TURF CAPACITY(4,1)\|SYNTHETIC TURF MANUFACTURING(4,1)\|CARBON DIOXIDE(3,10)\|GROUND(3,3)\|STONE BASE LAYER(3,3)\|BAMBOO(3,1)\|CARBON CAPTURE BENEFIT(3,1)\|CARBONACEOUS MINERAL MATERIAL(3,1)\|CYPRESS(3,1)\|ELASTOMER(3,1)\|ENGINEERING(3,1)\|EQUILIBRIUM(3,1)\|EXHIBIT SUPERIOR MECHANICAL PERFORMANCE(3,1)\|GRAINING(3,1)\|GROOMER(3,1)\|HEARTWOOD(3,1)\|IDENTIFICATION(3,1)\|	(US20250297409)\|1. A synthetic turf system comprising:\| a backing;\| turf fibers extended upward from the backing;\| one or more infill layers positioned above the backing, below a top portion of the turf fibers;\| wherein the one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|2. The synthetic turf system of claim 1, wherein the carbon sequestration sand includes wollastonite, basalt, peridotite, dunite, limestone, or dolostone.\|3. The synthetic turf system of claim 1, wherein the carbon sequestration sand is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the carbon sequestration sand chemically react with each other, forming a carbonate or a bicarbonate.\|4. The synthetic turf system of claim 1, wherein the carbon sequestration sand has a particle size of about #4 mesh to about #270 mesh, and is deposited in a layer having a thickness of about 1/16 to about ¼ inches above or below each of the one or more infill layers.\|5. The synthetic turf system of claim 1, wherein 90 percent of the carbon sequestration sand is small enough to pass through a #40 mesh screen, but too large to pass through an #80 mesh screen.\|6. The synthetic turf system of claim 1, wherein the one or more infill layers include the carbon sequestration sand,\| the one or more infill layers are disposed on top of the backing, between the turf fibers, and\| the top portion of the turf fibers extends above the one or more infill layers.\|7. The synthetic turf system of claim 1, wherein the backing is water permeable with a porosity that filters rainwater from the carbon sequestration sand and the one or more infill layers by gravity as the rainwater travels from the one or more infill layers to below the backing.\|8. The synthetic turf system of claim 1, further comprising a first base stone layer disposed below the backing, and a second base stone layer disposed below the first base stone layer, wherein the first base stone layer or the second base stone layer includes silicate rock, ultramafic rock, or reactive rock that is accessible to rainwater by gravity from the top portion of the turf fibers.\|9. The synthetic turf system of claim 8, wherein the carbon sequestration sand is positioned on, above, or in the first base stone layer or the second base stone layer.\|10. The synthetic turf system of claim 8, wherein the carbon sequestration sand is positioned below the second base stone layer, tilled into a subgrade below the second base stone layer, or positioned in a subdrain below the second base stone layer.\|11. The synthetic turf system of claim 8, wherein the first base stone layer or the second base stone layer is water permeable, and the carbon sequestration sand is blended into the first base stone layer or the second base stone layer.\|12. Infill for a synthetic turf system, the infill comprising:\| carbon sequestration sand including silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh; and\| organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|13. The carbon sequestration sand of claim 12, wherein 90 percent of the carbon sequestration sand is small enough to pass through a #40 mesh screen.\|14. The carbon sequestration sand of claim 13, wherein 90 percent of the carbon sequestration sand is too large to pass through an #80 mesh screen.\|15. The carbon sequestration sand of claim 12, wherein the silicate rock, ultramafic rock, or reactive rock is at least one of wollastonite, basalt, peridotite, dunite, limestone, and dolostone.\|16. The carbon sequestration sand of claim 12, wherein the silicate rock, ultramafic rock, or reactive rock forms weathered particles having a sphericity of about 0.65 to about 0.85.\|17. A method of preparing a synthetic turf system, the method comprising:\| dispersing carbon sequestration sand over a top portion of turf fibers, wherein the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|18. The method of claim 17, further comprising:\| grooming the carbon sequestration sand into the one or more infill layers of the synthetic turf system, between the turf fibers, at a backing of the synthetic turf system.\|19. The method of claim 17, further comprising:\| preblending the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the carbon sequestration sand over the top portion of the turf fibers.\|20. The method of claim 17, further comprising:\| measuring an aspect of the synthetic turf system, including a thickness of an infill layer, an acidity of rainwater at the infill layer, or a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer; and\| dispersing a predetermined quantity of the carbon sequestration sand over the top portion of the turf fibers as a top dressing based on the measured aspect.	(US20250297409)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] The application claims priority to and the benefit of U.S. Provisional Patent Application No. 63/569,558, filed on Mar. 25, 2024, entitled “Carbon Capture System and Method for Synthetic Turf Fields”, which we incorporate by reference in its entirety.\|(US20250297409)\|BACKGROUND\|[0002] Artificial or synthetic turf fields are composed of three primary components—from bottom to top: shock pad, carpet, and infill. These components are generally assembled on top of a base of compacted stone. The shock pad is optional and serves to convey much of the shock absorption performance of the turf field, required for the safety of those playing on the surface in the case of impact with the surface. The carpet serves to mimic the blades of grass and root zone, conveying the softness and traction of the surface as well as many of the ball interaction properties. The infill is generally constituted of at least two layers, the bottom layer of which serves to weight down and stabilize the carpets that it is laid onto, whereas the top layers serve as an additional interface layer to those playing on the field, conveying surface softness, friction, traction, and much of the mechanical properties of the field that are felt directly by the players.\|[0003] As a matter of background, a significant amount of engineering and development is devoted to developing artificial turf field systems. With respect to the infill, each kind of material has its own performance and structural characteristics. Obtaining the right composition and arrangement of materials can be challenging.\|[0004] Furthermore, when installation of a synthetic turf field occurs, generally speaking, a living, natural turf field is being replaced with an artificial one. In this process, a living organism, e.g., grass, plants, etc., which naturally removes carbon dioxide from the atmosphere is removed. Additionally, the construction associated with a synthetic turf field, as well as the actual manufacturing of the synthetic turf, result in additional carbon entering the atmosphere.\|[0005] As such, there remains a need for environmentally friendly and ultimately carbon-neutral or carbon-offsetting infill materials that present good mechanical properties and mechanical resistance, while presenting high availability, easy transportation, and low cost.\|SUMMARY\|[0006] The following presents a simplified summary to provide a basic understanding of some aspects of the disclosed subject matter. This summary is not an extensive overview. It is not intended to identify key/critical elements or to delineate the scope of the claimed subject matter. Its sole purpose is to present some concepts in a simplified form as a prelude to the more detailed description presented later.\|[0007] According to one aspect, a synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further includes a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|[0008] According to another aspect, infill for a synthetic turf system includes carbon sequestration sand. The carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh. The synthetic turf system may also includes organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|[0009] According to another aspect, a method of preparing a synthetic turf system includes dispersing carbon sequestration sand over a top portion of turf fibers, where the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a bicarbonate or carbonate with rainwater traveling through infill.\|[0010] In other aspects, a carbon sequestration sand-based infill employs a shock pad to achieve a desired and/or proper shock absorption on the turf. The carbon sequestration sand-based infill is most often installed over a layer of permeable backing, where the carbon sequestration sand acts as a stabilizing infill or as part of a stabilizing infill layer. As a stabilizing infill, the carbon sequestration sand performs as a ballast layer that weighs down the turf carpets and mitigates movement.\|[0011] In other aspects, an infill composition for artificial turf fields includes at least one layer of carbon sequestration sand. The carbon sequestration sand includes a particle size distribution of carbon sequestration sand with a size of approximately #4 mesh to #270 mesh. The infill can be installed according to a method of spreading a layer of carbon sequestration sand over a carpet that is on a base of compacted stone. The layers of the carbon sequestration sand are brushed and de-compacted such that the carbon sequestration sand is evenly distributed over the carpet of the turf system.\|[0012] In other aspects, a carbon sequestration sand-based layer may be positioned immediately below the shock pad (if used), on top of the substrate material, e.g., a rock layer. In such a position, the carbon sequestration sand-based layer may have a thickness of 1/16″ to ¼″, with a mesh size in the range of #4 to #270.\|[0013] In still other aspects, carbon sequestration sand may be blended into a stone base layer positioned immediately below the shock pad (if so equipped). In some embodiments, the carbon sequestration sand may be blended into a first of two topping stone base layer system. In other embodiments, the carbon sequestration sand may be blended into some or all of a stone base layer system.\|[0014] In yet another aspect, a layer of carbon sequestration sand may be positioned on a geotextile or subgrade layer. In such a position, the carbon sequestration sand-based layer may have a thickness of 1/16″ to ¼″, with a mesh size in the range of about #4 to #270.\|[0015] In still yet another aspect, carbon sequestration sand may be tilled or blended into native subgrade material. In such a position, the carbon sequestration sand may be blended within the subgrade, e.g., soil, as discussed below.\|[0016] In each of the foregoing aspects, certain carbon sequestration processes can occur as rainwater interacts with the carbon sequestration sand, regardless of the position in the artificial turf system. Further discussion of the processes referenced above are included in the following description.\|[0017] The innovation described herein introduces a carbon sequestration sand-based infill material designed to enhance the mechanical performance or environmental sustainability of synthetic turf systems. The infill material offers ease of application across various layers of the turf system and provides stabilization of the turf fibers while supporting upright positioning. When dispersed over the turf system as a top dressing or integrated within infill layers, the carbon sequestration sand performs as a ballast that mitigates infill migration and enhances field durability. Additionally, the material facilitates carbon capture through chemical reactions with rainwater, enabling the formation of bicarbonates or carbonates that contribute to carbon sequestration while maintaining desired surface properties such as traction, softness, and shock absorption.\|[0018] To the accomplishment of the foregoing and related ends, certain illustrative aspects of the claimed subject matter are described herein in connection with the following description and the annexed drawings. These aspects indicate various ways in which the subject matter may be practiced, all of which are intended to be within the scope of the disclosed subject matter. Other advantages and novel features may become apparent from the following detailed description when considered in conjunction with the drawings.\|[0019] These and other systems, methods, objects, features, and advantages of the present disclosure will be apparent to those skilled in the art from the following detailed description of the preferred embodiment and the drawings.\|[0020] All documents mentioned herein are hereby incorporated in their entirety by reference. References to items in the singular should be understood to include items in the plural, and vice versa, unless explicitly stated otherwise or clear from the text. Grammatical conjunctions are intended to express any and all disjunctive and conjunctive combinations of conjoined clauses, sentences, words, and the like, unless otherwise stated or clear from the context.\|(US20250297409)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0021] FIG. 1 is a partial perspective view of an example synthetic turf system having an infill made of carbon sequestration sand in accordance with some embodiments of the present disclosure.\|[0022] FIG. 2 is a perspective view of an example application system employed in dispersing the carbon sequestration sand over the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0023] FIG. 3 is a perspective view of an example brush employed in grooming the sand into the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0024] FIG. 4 is a partial perspective view of the synthetic turf system of FIG. 1, where an infill made of the carbon sequestration sand in accordance with some embodiments of the present disclosure.\|[0025] FIG. 5 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand layered below a backing in accordance with some embodiments of the present disclosure.\|[0026] FIG. 6 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is blended into a base stone layer in accordance with some embodiments.\|[0027] FIG. 7 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is layered on a geotextile in accordance with some embodiments.\|[0028] FIG. 8 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is diffused into a subgrade in accordance with some embodiments.\|[0029] FIG. 9 is an example process flow for preparing the synthetic turf system of FIG. 1.\|(US20250297409)\|DETAILED DESCRIPTION\|[0030] Various aspects of the subject disclosure are now described in more detail with reference to the annexed drawings, wherein like numerals generally refer to like or corresponding elements throughout. It should be understood, however, that the drawings and detailed description relating thereto are not intended to limit the claimed subject matter to the particular form disclosed. Instead, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the described and claimed subject matter.\|[0031] The following disclosure provides many different embodiments, or examples, for implementing different features of the provided subject matter. Specific examples of components and arrangements are described below to simplify the present disclosure. These are, of course, merely examples and are not intended to be limiting. For example, the formation of a first feature over or on a second feature in the description that follows may include embodiments in which the first and second features are formed in direct contact, and may also include embodiments in which additional features may be formed between the first and second features, such that the first and second features may not be in direct contact. In addition, the present disclosure may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.\|[0032] Further, spatially relative terms, such as “beneath,” “below,” “lower,” “above,” “upper” and the like, may be used herein for ease of description to describe one element or feature's relationship to another element(s) or feature(s) as illustrated in the figures. The spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. The apparatus may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein may likewise be interpreted accordingly.\|[0033] Numerical values in the specification and claims of this application should be understood to include numerical values which are the same when reduced to the same number of significant figures and numerical values which differ from the stated value by less than the experimental error of conventional measurement technique of the type described in the present application to determine the value. All ranges disclosed herein are inclusive of the recited endpoint.\|[0034] The term “about” can be used to include any numerical value that can vary without changing the basic function of that value. When used with a range, “about” also discloses the range defined by the absolute values of the two endpoints, e.g., “about 2 to about 4” also discloses the range “from 2 to 4.” The term “about” may refer to plus or minus 10% of the indicated number.\|[0035] In accordance with varying embodiments discussed herein, there is provided an artificial turf system that utilizes a material derived from one or more types of carbon sequestration sands, including, for example and without limitation, wollastonite sand (general formula CaSiO3), limestone, basalt, or the like. More specifically, the carbon sequestration sands may be formed from silicate rock, ultramafic rock, or reactive rock, and specifically include, for example, wollastonite, basalt, peridotite, olivine, dunite, limestone, and dolostone.\|[0036] In some embodiments, the carbon sequestration sand may be used as an infill material, an intervening layer of material between existing layers of the system, mixed within a particular layer, on or mixed within a substrate, or combinations thereof.\|[0037] In addition to its excellent performance on the field, this carbon sequestration sand also exhibits behaviors that provide for carbon sequestration. Specifically, the material, when in contact with rainwater, causes a chemical reaction to occur between carbonic acid naturally present in the rainwater and the sand, e.g., olivine, wollastonite, etc. The reaction weathers the olivine, wollastonite, etc., and converts the carbonic acid into bicarbonate or carbonate. In this regard, carbonate and bicarbonate tend to be in equilibrium in aqueous solutions caused by weathering reactions because the dissolution of carbon dioxide and minerals generates a dynamic balance governed by pH-dependent acid-base reactions.\|[0038] By converting the carbon dioxide into other substances, the carbon dioxide can no longer be released into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These bicarbonate or carbonate solutions are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments, as well as integrated into marine animal carbonaceous mineral materials. These carbonate sediments form a sink for carbon dioxide.\|[0039] An example implementation of the embodiment described above is shown in FIG. 1. In this regard, FIG. 1 depicts a portion of a synthetic turf system 100 including carbon sequestration sand 102 that may be olivine-based, wollastonite-based, etc. and is utilized in one or more layers of infill materials. In accordance with some embodiments, the carbon sequestration sand 102 may be deposited in a layer having a thickness of about 1/16 to about ¼ inches, and have a particle size of about #4 mesh to about #270 mesh in the U.S. Standard Sieve Series. As will be appreciated, mesh may be defined as the number of openings in one square inch of a screen. A large mesh number means the pores in the screen are small. Sand's mesh size is determined by graining, and the numbers refer to the maximum and minimum grain diameters. 40/80 sand means that 90 percent of the sand by volume is small enough to pass through a #40 mesh screen, but too large to pass through an #80 mesh screen. As such, the range of particle size of the carbon sequestration sand 102 referenced in FIG. 1 may be about #4 mesh (4,750 μm) to about #270 mesh (53 μm).\|[0040] As shown in FIG. 1, the portion of the synthetic turf system 100 includes one or more infill layers 104 (described below), a permeable (e.g., carpet) backing 110, and turf fibers 112 that are artificial grass blades extended substantially perpendicular to the backing 110. With this construction, when the backing 110 is extended flatly in a horizontal direction, such as a stone base layer described in greater detail below, the turf fibers 112 may extend upward in a vertical direction perpendicular to the horizontal direction. While, as depicted, the turf fibers 112 are artificial grass blades, the turf fibers 112 may additionally or alternatively include natural grass blades extended upward from the backing 110, through the carbon sequestration sand 102 and the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0041] The infill layers 104 are positioned above the backing 110, in between the turf fibers 112, and below a top portion 114 of the turf fibers 112. More specifically, the infill layers 104 are disposed directly on top of the backing 110, where the top portion 114 of the turf fibers 112 extends above the infill layers 104. While, as depicted, the example embodiment of FIG. 1 includes multiple layers of infill materials respectively shown as a first layer 120, a second layer 122, and a third layer 124, the synthetic turf system 100 may include more or fewer distinct infill layers. Also, while, as depicted, the carbon sequestration sand 102 is disposed below the third layer 124 and directly contacts the backing 110, where the carbon sequestration sand 102 is interposed between and separates the infill layers 104 from the backing 110, the carbon sequestration sand 102 may additionally or alternatively be incorporated into the first layer 120, the second layer 122, or the third layer 124, or be applied over the third layer 124 as a top dressing of the synthetic turf system 100 without departing from the scope of the present disclosure.\|[0042] In this regard, the carbon sequestration sand 102 may partially or entirely form the first layer 120, the second layer 122, or the third layer 124 with a variety of compositional ranges. In an embodiment, the carbon sequestration sand 102 forms up to 90 percent of the first layer 120, the second layer 122, or the third layer 124 by volume. In a further embodiment, the carbon sequestration sand 102 forms up to 10 percent of the first layer 120, the second layer 122, or the third layer 124 by volume. With this construction, water insoluble components of the first layer 120, the second layer 122, or the third layer 124 reduce an overall wear rate of the synthetic turf system 100, and maintain a minimum volume in the synthetic turf system 100. In this manner, a wear rate and minimum volume of the first layer 120, the second layer 122, or the third layer 124 may be adjusted as desired by adjusting the compositional range of the carbon sequestration sand 102. In an embodiment, the carbon sequestration sand 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0043] The weathering rate and shape of particles forming the carbon sequestration sand 102 are influenced by material selection and particle size distribution. In this regard, consistent particle sizing promotes uniform weathering rates across the one or more infill layers 104, maintaining overall field performance and carbon sequestration efficiency in the synthetic turf system 100. The carbon sequestration sand 102 is accessible to rainwater traveling downward by gravity from the top portion 114 of the turf fibers 112 toward the backing 110. As the carbon sequestration sand 102 weathers through exposure to rainwater, its constituent particles may substantially change morphology, or alternatively may remain largely the same shape. In embodiments, the selected silicate rock, ultramafic rock, or reactive rock materials form weathered particles that maintain a sphericity of about 0.65 to about 0.85. This sphericity range supports stable packing within the synthetic turf system, reduces compaction variability, and ensures continued mechanical performance while facilitating consistent chemical reactions for carbon capture.\|[0044] In an embodiment where the carbon sequestration sand 102 is incorporated in the synthetic turf system 100 as a top dressing, the carbon sequestration sand 102 is periodically dispersed over the top portion 114 of the turf fibers 112 with an application system 130 depicted in FIG. 2. With continued reference to FIG. 2, the application system 130 includes a seed tender 132 and a tractor 134 that disperses the carbon sequestration sand 102 over the synthetic turf system 100 from a broadcaster tool 140. The seed tender 132 is employed in conjunction with a hydraulically-controlled conveyor 142 and a hopper gate 144, which supply the tractor 134 the carbon sequestration sand 102. As the tractor 134 moves at a consistent speed across the synthetic turf system 100 following a predetermined pattern, the hydraulically-controlled conveyor 142 and the hopper gate 144 precisely control a flow rate of the carbon sequestration sand 102 to the tractor 134, ensuring uniform distribution across the synthetic turf system 100.\|[0045] While, as depicted, the application system 130 includes the broadcaster tool 140 pulled by the tractor 134, and continuously fed the carbon sequestration sand 102 by the seed tender 132 along or across the synthetic turf system 100, the application system 130 may additionally or alternatively include a variety of components configured to spread granular material across a field, such as, for example, a self-propelled, manually powered, or power take-off (PTO) driven broadcast material spreader, a pneumatic spreader, an air boom spreader, a drop spreader, a handheld spreader, or an aerial spreader for dispersing the carbon sequestration sand 102 without departing from the scope of the present disclosure.\|[0046] Once the carbon sequestration sand 102 is dispersed across the synthetic turf system 100 by the application system 130, the carbon sequestration sand 102 is brushed into the one or more infill layers 104, including the first layer 120, the second layer 122, and the third layer 124. In this regard, a brush 150 depicted in FIG. 3 grooms the carbon sequestration sand 102 into the one or more infill layers 104. Rotary brush action on the synthetic turf system 100 from the top portion 114 by the brush 150 effectively works the carbon sequestration sand 102 downward between the turf fibers 112, ensuring proper placement within the infill material forming the one or more infill layers 104, while maintaining structural integrity and performance characteristics of the synthetic turf system 100, including at the top portion 114 and the first layer 120.\|[0047] While, as depicted, the brush 150 is a motorized, walk-behind rotary brush apparatus, such as a Shindaiwa or Laymor brush system, the brush 150 may additionally or alternatively include various components for incorporating the carbon sequestration sand 102 into the one or more infill layers 104 such as, for example, a ride-on turf groomer, a tractor-mounted brush that is dragged or PTO driven, or manual turf brushing equipment. Furthermore, brushes employed in such configurations may embody various shapes, sizes, and types, such as, for example, straight brushes, triangular brushes, hydraulic brushes, oscillating brushes, rigid brushes, flexible brushes, or brush assemblies including at least one plurality of brushes. Furthermore, the brush 150 may additionally or alternatively include specialty turf equipment, such as a vacuum or other devices complementary to the brush 150, and utilized to integrate the carbon sequestration sand 102 into the existing infill material of the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0048] Referring back to FIG. 1, infill is representative of material that is deposited over the backing 110 and forms the one or more infill layers 104 around the turf fibers 112. Infill is interspersed between the turf fibers 112 rising out of the backing 110. Infill generally has a depth that covers a portion of the turf fibers 112 (unexposed portion of the artificial fibers/blades) leaving part of the turf fibers 112, i.e., the top portion 114 extending above the infill (exposed portion of the artificial fibers/blades).\|[0049] In accordance with some embodiments, the one or more infill layers 104 assists in supporting the turf fibers 112 in an upright position and is used to provide traction and shock absorption. As a general matter, various types of infill arrangements are contemplated. For example, two layer, three layers, or other arrangements are contemplated. For convenience, the present description primarily discusses two and three layer embodiments.\|[0050] In some embodiments, the first layer 120 may include, for example and without limitation, heartwood or sapwood portions of hardwood or softwood, such as bamboo, cypress, poplar, pine, and cedar. The first layer 120 may additionally or alternatively include, for example and without limitation, cork, corn cobs, olive pits, barks, coconut peat or other organic materials, as well as styrene-butadiene rubber (SBR) particles ethylene propylene diene monomer (EPDM) rubber, other thermoplastics such as polyethylene, polypropylene, or composite materials can be used that combine thermoplastics, elastomers, reinforcements and/or fillers or other sufficient material. In accordance with some embodiments, the second layer 122 of infill material depicted in FIG. 1 may include a mixture of materials, e.g., material of the first layer 120 and a sand material. In such embodiments, the third layer 124 of infill material may include the aforementioned sand material, such that the fourth or lowermost layer is that of the carbon sequestration sand 102.\|[0051] In accordance with some embodiments, a shock pad (not shown) may be employed to achieve a desired shock absorption in accordance with a particular installation/purpose. For example, a shock pad (not shown) may be positioned below the one or more infill layers 104 shown in FIG. 1. As such, the material of the infill layers 104 conveys many of the mechanical properties that may be desired for use as artificial turf infill.\|[0052] In some embodiments, the carbon sequestration sand 102 can be used in combination with the backing 110, and/or a stabilizing infill layer (e.g., sand) 104 to make up the synthetic turf system 100. The synthetic turf system 100, using the described infill material, exhibits superior mechanical performance, a greater mechanical durability, easy availability and mitigates or otherwise avoids issues of floating away when subjected to large amounts of water.\|[0053] In some other embodiments, the backing 110 may be positioned below the carbon sequestration sand 102 shown in FIG. 1. In such embodiments, the backing 110 may correspond to the material into which the turf fibers 112 are woven, held, inserted, etc. Accordingly, the carbon sequestration sand 102 is positioned directly on the backing 110, thereby functioning as a ballast layer. The backing 110 is water permeable, without punched holes, such that the carbon sequestration sand 102 may remain in place at the backing 110, underlying the remainder of the infill layers 104, thereby maximizing contact with rainwater while preventing the carbon sequestration sand 102 from being flushed out of the synthetic turf system 100 via regular drainage measures. More specifically, the backing 110 has a porosity that filters rainwater from the carbon sequestration sand 102 and the one or more infill layers 104 as the rainwater travels downward through the synthetic turf system 100 from the one or more infill layers 104 to below the backing 110.\|[0054] Turning now to FIG. 4, there is shown a more detailed three-dimensional cross-sectional view of a portion of the synthetic turf system 100 utilizing the carbon sequestration sand 102 as a ballast infill material in accordance with the embodiment set forth above in FIG. 1. It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|[0055] As shown in FIG. 4, the synthetic turf system 100, in addition to including the turf fibers 112, the carbon sequestration sand 102, the infill layers 104, and the backing 110, further includes a first base stone layer 200 disposed below the backing 110 and above a second base stone layer 202. The synthetic turf system 100 further includes a geotextile component 204 that is a fabric disposed between the second base stone layer 202 and a subgrade 210. The synthetic turf system 100 may further include a subdrain trench component 212 formed in the subgrade and housing a drainage pipe 214.\|[0056] As discussed above, the carbon sequestration sand 102 may be implemented, for example and without limitation, olivine, wollastonite, basalt, limestone, etc. In operation, with reference to FIGS. 1 and 4, as rainwater contacts the carbon sequestration sand 102, a chemical reaction occurs between carbonic acid naturally present in the rainwater and the sequestration sand. The reaction weathers the carbon sequestration sand 102, e.g., olivine, wollastonite, etc., and converts the carbonic acid into carbonate or bicarbonate. As stated above, the conversion of the carbon dioxide into other substances prevents the release of the carbon dioxide into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. Carbonate and bicarbonate solutions may permeate the first base stone layer 200 and the second base stone layer 202, through the geotextile component 204 and into the subdrain trench component 212 and drainage pipe 214. Thereafter, the carbonate and bicarbonate solutions are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments, forming a sink for carbon dioxide.\|[0057] Turning now to FIG. 5, there is shown another embodiment of the synthetic turf system 100 utilizing the carbon sequestration sand 102. As illustrated in FIG. 5, the carbon sequestration sand 102 is applied on a top surface of the first base stone layer 200, below the backing 110. Application may be made via a suitable top-dressing machine, such as the application system 130 depicted in FIG. 2. In the embodiment of FIG. 5, the carbon sequestration sand 102 may be deposited with a thickness in the range of about 1/16″ to ¼″. The carbon sequestration sand 102 of FIG. 5 may be implemented with a particle size of about #4 mesh to #270 mesh. In such an embodiment, rainwater would flow directly through the one or more infill layers 104, the backing 110, and the carbon sequestration sand 102 and into the first base stone layer 200. Reaction with the rainwater would occur as described above with respect to FIGS. 1 and 4.\|[0058] With reference now to FIG. 6, there is illustrated the synthetic turf system 100 utilizing particles of the carbon sequestration sand 102 in accordance with another embodiment. In the embodiment depicted in FIG. 6, particles of the carbon sequestration sand 102 are incorporated into the first base stone layer 200. In accordance with one non-limiting example, the first base stone layer 200 may be implemented as a layer of stone having a thickness in the range of about 1 inch to about 6 inches, and in some particular embodiments, in the range of about 1 inch to about 2 inches. In such embodiments, the first base stone layer 200 may include for example and without limitation, a suitable drainage stone, such as gravel (e.g., granite) or the like. The carbon sequestration sand 102 may be suitably mixed with the stone to distribute the carbon sequestration sand 102 throughout the first base stone layer 200. In some embodiments, a single, e.g., uniform, base stone layer (not shown) may be utilized. In such embodiments, the carbon sequestration sand 102 may be blended into the single base stone layer, e.g., to a certain depth thereof (e.g., the top 1″ or 2″ thereof), or throughout the base stone layer. As described in greater detail above, reaction of the carbon sequestration sand 102 with rainwater would occur as described above with respect to FIGS. 1, 4, and 5.\|[0059] Turning now to FIG. 7, there is shown another embodiment of the synthetic turf system 100 utilizing carbon sequestration sand 102. As illustrated in FIG. 7, the carbon sequestration sand 102 may be on the geotextile component 204. In such a position, the carbon sequestration sand 102 may form a layer having a thickness of about 1/16″ to about ¼″, with a mesh size in the range of about #4 to about #270. Stated another way, the layer of carbon sequestration sand 102 may be applied at a bottom of the second base stone layer 202, as shown in FIG. 7. In accordance with one non-limiting example, the second base stone layer 202 may be implemented as a layer of stone having a thickness in the range of about 2 inches to about 6 inches, and in some particular embodiments, in the range of about 3 inches to about 4 inches. In such embodiments, the second base stone layer 202 may include, for example and without limitation, a suitable drainage stone, such as gravel (e.g., granite) or the like.\|[0060] In an embodiment, the first base stone layer 200 or the second base stone layer 202 includes silicate rocks, ultramafic rocks, or otherwise reactive rocks such as, for example, basalt, peridotite, olivine, dunite, limestone, and dolostone. Notably, in such an embodiment, the first base stone layer 200 or the second base stone layer 202 may perform carbon sequestration upon weathering by rainwater, in addition to the carbon sequestration sand 102, increasing an overall carbon sequestration capacity of the synthetic turf system 100.\|[0061] Although not shown, it is contemplated that the carbon sequestration sand 102 may be blended with the stone of the second base stone layer 202 similar to the manner described above with respect to FIG. 6. Similarly, although not illustrated in the accompanying figures, it is further contemplated that the carbon sequestration sand 102 may be blended with the stone of the subdrain trench component 212, or layered in the subdrain trench component 212 without blending. The above described positions of the carbon sequestration sand 102 would also enable the carbon capture reaction described above with respect to FIGS. 1 and 4-6.\|[0062] Referring now to FIG. 8, there is shown the synthetic turf system 100 utilizing the carbon sequestration sand 102 in accordance with another embodiment. As illustrated in FIG. 8, the carbon sequestration sand 102 may be tilled and incorporated into the subgrade 210 of the synthetic turf system 100, e.g., soil, sediment, etc. In such an implementation, the geotextile component 204 layered over the subgrade 210, and a 6″ to 8″ combined thickness of the first base stone layer 200 and the second base stone layer 202 may be installed on the subgrade 210 with the carbon sequestration sand 102 distributed therein. It will be appreciated that more carbon sequestration sand 102 may be used with this embodiment than the embodiments described above, thereby providing the synthetic turf system 100 additional carbon sequestration capability.\|[0063] Furthermore, it will be appreciated that by placing the carbon sequestration sand 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air. That is, as organic matter breaks down it creates additional carbon dioxide. As such, having the carbon sequestration sand 102 in the subgrade 210 where there is potential for more water availability increases the ability for the weathering reaction to occur, thereby facilitating carbon sequestration. In addition, as described above with respect to FIGS. 1 and 4-7, rainwater reaction with the carbon sequestration sand 102 provides the aforementioned carbon capture benefits.\|[0064] Referring to FIG. 9, a method 300 for preparing a synthetic turf system will be described according to an exemplary embodiment. FIG. 9 will be described with reference to FIGS. 1-8. For simplicity, the method 300 will be described as a sequence of blocks, but the elements of the method 300 can be organized into different architectures, elements, stages, and/or processes.\|[0065] At block 302, the method 300 includes measuring an aspect of the synthetic turf system 100. More specifically, a user may measure a thickness of an infill layer, such as one of the infill layers 104, may measure an acidity of rainwater at the infill layer, and may measure a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer.\|[0066] At block 304, the method 300 includes preblending or layering the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112. In an embodiment, the method 300 includes determining desired compositional ranges of the carbon sequestration sand 102 based on the measurement or measurements taken at block 302. In this manner, the wear rate and the minimum volume of the one or more infill layers 104 is controlled by adjusting the compositional ranges of components of the carbon sequestration sand 102. In an embodiment, the carbon sequestration sand 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0067] At block 310, the method 300 includes dispersing the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112, where the carbon sequestration sand 102 includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through the one or more infill layers 104 by gravity. In an embodiment, dispersing the carbon sequestration sand 102 includes dispersing a predetermined quantity of the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112 as a top dressing based on the measurement taken at block 302.\|[0068] At block 312, the method 300 includes grooming the carbon sequestration sand 102 into the one or more infill layers 104 of the synthetic turf system 100, between the turf fibers 112, at the backing 110 of the synthetic turf system 100. In this regard, the brush 150 grooms the carbon sequestration sand 102 into and through the one or more infill layers 104, where the carbon sequestration sand 102 contacts and rests on the backing 110.\|[0069] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions and/or alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc., do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.\|[0070] While specific embodiments are shown and described herein, it is contemplated that alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc. without departing from the spirit and/or scope of the innovation as described in detail. These alternative embodiments are to be included within the spirit and scope of the innovation as described and claimed herein.\|[0071] Although the subject matter has been described in language specific to structural features or methodological acts, it is to be understood that the subject matter of the appended claims is not necessarily limited to the specific features or acts described above. Rather, the specific features and acts described above are disclosed as example aspects.\|[0072] Various operations of aspects are provided herein. The order in which one or more or all of the operations are described should not be construed as to imply that these operations are necessarily order dependent. Alternative ordering will be appreciated based on this description. Further, not all operations may necessarily be present in each aspect provided herein.\|[0073] As used in this application, “or” is intended to mean an inclusive “or” rather than an exclusive “or”. Further, an inclusive “or” may include any combination thereof (e.g., A, B, or any combination thereof). In addition, “a” and “an” as used in this application are generally construed to mean “one or more” unless specified otherwise or clear from context to be directed to a singular form. Additionally, at least one of A and B and/or the like generally means A or B or both A and B. Further, to the extent that “includes”, “having”, “has”, “with”, or variants thereof are used in either the detailed description or the claims, such terms are intended to be inclusive in a manner similar to the term “comprising”.\|[0074] Further, unless specified otherwise, “first”, “second”, or the like are not intended to imply a temporal aspect, a spatial aspect, an ordering, etc. Rather, such terms are merely used as identifiers, names, etc. for features, elements, items, etc. For example, a first channel and a second channel generally correspond to channel A and channel B or two different or two identical channels or the same channel. Additionally, “comprising”, “comprises”, “including”, “includes”, or the like generally means comprising or including, but not limited thereto.\|[0075] Further, the term “in” as used to describe an object with respect to a given direction (e.g., an edge extended in a left-right direction) is intended to denote an orientation that is substantially parallel to the specified direction. In contrast, the term “along” as used to describe an object with respect to a given direction (e.g., an edge extended along a vertical direction) is intended to indicate that a feature or element possesses a common vector component in that direction, even if its overall alignment is not strictly parallel.\|[0076] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.	(US20250297409)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] The application claims priority to and the benefit of U.S. Provisional Patent Application No. 63/569,558, filed on Mar. 25, 2024, entitled “Carbon Capture System and Method for Synthetic Turf Fields”, which we incorporate by reference in its entirety.\|(US20250297409)\|BACKGROUND\|[0002] Artificial or synthetic turf fields are composed of three primary components—from bottom to top: shock pad, carpet, and infill. These components are generally assembled on top of a base of compacted stone. The shock pad is optional and serves to convey much of the shock absorption performance of the turf field, required for the safety of those playing on the surface in the case of impact with the surface. The carpet serves to mimic the blades of grass and root zone, conveying the softness and traction of the surface as well as many of the ball interaction properties. The infill is generally constituted of at least two layers, the bottom layer of which serves to weight down and stabilize the carpets that it is laid onto, whereas the top layers serve as an additional interface layer to those playing on the field, conveying surface softness, friction, traction, and much of the mechanical properties of the field that are felt directly by the players.\|[0003] As a matter of background, a significant amount of engineering and development is devoted to developing artificial turf field systems. With respect to the infill, each kind of material has its own performance and structural characteristics. Obtaining the right composition and arrangement of materials can be challenging.\|[0004] Furthermore, when installation of a synthetic turf field occurs, generally speaking, a living, natural turf field is being replaced with an artificial one. In this process, a living organism, e.g., grass, plants, etc., which naturally removes carbon dioxide from the atmosphere is removed. Additionally, the construction associated with a synthetic turf field, as well as the actual manufacturing of the synthetic turf, result in additional carbon entering the atmosphere.\|[0005] As such, there remains a need for environmentally friendly and ultimately carbon-neutral or carbon-offsetting infill materials that present good mechanical properties and mechanical resistance, while presenting high availability, easy transportation, and low cost.\|SUMMARY\|[0006] The following presents a simplified summary to provide a basic understanding of some aspects of the disclosed subject matter. This summary is not an extensive overview. It is not intended to identify key/critical elements or to delineate the scope of the claimed subject matter. Its sole purpose is to present some concepts in a simplified form as a prelude to the more detailed description presented later.\|[0007] According to one aspect, a synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further includes a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|[0008] According to another aspect, infill for a synthetic turf system includes carbon sequestration sand. The carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh. The synthetic turf system may also includes organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|[0009] According to another aspect, a method of preparing a synthetic turf system includes dispersing carbon sequestration sand over a top portion of turf fibers, where the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a bicarbonate or carbonate with rainwater traveling through infill.\|[0010] In other aspects, a carbon sequestration sand-based infill employs a shock pad to achieve a desired and/or proper shock absorption on the turf. The carbon sequestration sand-based infill is most often installed over a layer of permeable backing, where the carbon sequestration sand acts as a stabilizing infill or as part of a stabilizing infill layer. As a stabilizing infill, the carbon sequestration sand performs as a ballast layer that weighs down the turf carpets and mitigates movement.\|[0011] In other aspects, an infill composition for artificial turf fields includes at least one layer of carbon sequestration sand. The carbon sequestration sand includes a particle size distribution of carbon sequestration sand with a size of approximately #4 mesh to #270 mesh. The infill can be installed according to a method of spreading a layer of carbon sequestration sand over a carpet that is on a base of compacted stone. The layers of the carbon sequestration sand are brushed and de-compacted such that the carbon sequestration sand is evenly distributed over the carpet of the turf system.\|[0012] In other aspects, a carbon sequestration sand-based layer may be positioned immediately below the shock pad (if used), on top of the substrate material, e.g., a rock layer. In such a position, the carbon sequestration sand-based layer may have a thickness of 1/16″ to ¼″, with a mesh size in the range of #4 to #270.\|[0013] In still other aspects, carbon sequestration sand may be blended into a stone base layer positioned immediately below the shock pad (if so equipped). In some embodiments, the carbon sequestration sand may be blended into a first of two topping stone base layer system. In other embodiments, the carbon sequestration sand may be blended into some or all of a stone base layer system.\|[0014] In yet another aspect, a layer of carbon sequestration sand may be positioned on a geotextile or subgrade layer. In such a position, the carbon sequestration sand-based layer may have a thickness of 1/16″ to ¼″, with a mesh size in the range of about #4 to #270.\|[0015] In still yet another aspect, carbon sequestration sand may be tilled or blended into native subgrade material. In such a position, the carbon sequestration sand may be blended within the subgrade, e.g., soil, as discussed below.\|[0016] In each of the foregoing aspects, certain carbon sequestration processes can occur as rainwater interacts with the carbon sequestration sand, regardless of the position in the artificial turf system. Further discussion of the processes referenced above are included in the following description.\|[0017] The innovation described herein introduces a carbon sequestration sand-based infill material designed to enhance the mechanical performance or environmental sustainability of synthetic turf systems. The infill material offers ease of application across various layers of the turf system and provides stabilization of the turf fibers while supporting upright positioning. When dispersed over the turf system as a top dressing or integrated within infill layers, the carbon sequestration sand performs as a ballast that mitigates infill migration and enhances field durability. Additionally, the material facilitates carbon capture through chemical reactions with rainwater, enabling the formation of bicarbonates or carbonates that contribute to carbon sequestration while maintaining desired surface properties such as traction, softness, and shock absorption.\|[0018] To the accomplishment of the foregoing and related ends, certain illustrative aspects of the claimed subject matter are described herein in connection with the following description and the annexed drawings. These aspects indicate various ways in which the subject matter may be practiced, all of which are intended to be within the scope of the disclosed subject matter. Other advantages and novel features may become apparent from the following detailed description when considered in conjunction with the drawings.\|[0019] These and other systems, methods, objects, features, and advantages of the present disclosure will be apparent to those skilled in the art from the following detailed description of the preferred embodiment and the drawings.\|[0020] All documents mentioned herein are hereby incorporated in their entirety by reference. References to items in the singular should be understood to include items in the plural, and vice versa, unless explicitly stated otherwise or clear from the text. Grammatical conjunctions are intended to express any and all disjunctive and conjunctive combinations of conjoined clauses, sentences, words, and the like, unless otherwise stated or clear from the context.\|(US20250297409)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0021] FIG. 1 is a partial perspective view of an example synthetic turf system having an infill made of carbon sequestration sand in accordance with some embodiments of the present disclosure.\|[0022] FIG. 2 is a perspective view of an example application system employed in dispersing the carbon sequestration sand over the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0023] FIG. 3 is a perspective view of an example brush employed in grooming the sand into the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0024] FIG. 4 is a partial perspective view of the synthetic turf system of FIG. 1, where an infill made of the carbon sequestration sand in accordance with some embodiments of the present disclosure.\|[0025] FIG. 5 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand layered below a backing in accordance with some embodiments of the present disclosure.\|[0026] FIG. 6 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is blended into a base stone layer in accordance with some embodiments.\|[0027] FIG. 7 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is layered on a geotextile in accordance with some embodiments.\|[0028] FIG. 8 is a partial perspective view of the synthetic turf system of FIG. 1, where the carbon sequestration sand is diffused into a subgrade in accordance with some embodiments.\|[0029] FIG. 9 is an example process flow for preparing the synthetic turf system of FIG. 1.\|(US20250297409)\|DETAILED DESCRIPTION\|[0030] Various aspects of the subject disclosure are now described in more detail with reference to the annexed drawings, wherein like numerals generally refer to like or corresponding elements throughout. It should be understood, however, that the drawings and detailed description relating thereto are not intended to limit the claimed subject matter to the particular form disclosed. Instead, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the described and claimed subject matter.\|[0031] The following disclosure provides many different embodiments, or examples, for implementing different features of the provided subject matter. Specific examples of components and arrangements are described below to simplify the present disclosure. These are, of course, merely examples and are not intended to be limiting. For example, the formation of a first feature over or on a second feature in the description that follows may include embodiments in which the first and second features are formed in direct contact, and may also include embodiments in which additional features may be formed between the first and second features, such that the first and second features may not be in direct contact. In addition, the present disclosure may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.\|[0032] Further, spatially relative terms, such as “beneath,” “below,” “lower,” “above,” “upper” and the like, may be used herein for ease of description to describe one element or feature's relationship to another element(s) or feature(s) as illustrated in the figures. The spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. The apparatus may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein may likewise be interpreted accordingly.\|[0033] Numerical values in the specification and claims of this application should be understood to include numerical values which are the same when reduced to the same number of significant figures and numerical values which differ from the stated value by less than the experimental error of conventional measurement technique of the type described in the present application to determine the value. All ranges disclosed herein are inclusive of the recited endpoint.\|[0034] The term “about” can be used to include any numerical value that can vary without changing the basic function of that value. When used with a range, “about” also discloses the range defined by the absolute values of the two endpoints, e.g., “about 2 to about 4” also discloses the range “from 2 to 4.” The term “about” may refer to plus or minus 10% of the indicated number.\|[0035] In accordance with varying embodiments discussed herein, there is provided an artificial turf system that utilizes a material derived from one or more types of carbon sequestration sands, including, for example and without limitation, wollastonite sand (general formula CaSiO3), limestone, basalt, or the like. More specifically, the carbon sequestration sands may be formed from silicate rock, ultramafic rock, or reactive rock, and specifically include, for example, wollastonite, basalt, peridotite, olivine, dunite, limestone, and dolostone.\|[0036] In some embodiments, the carbon sequestration sand may be used as an infill material, an intervening layer of material between existing layers of the system, mixed within a particular layer, on or mixed within a substrate, or combinations thereof.\|[0037] In addition to its excellent performance on the field, this carbon sequestration sand also exhibits behaviors that provide for carbon sequestration. Specifically, the material, when in contact with rainwater, causes a chemical reaction to occur between carbonic acid naturally present in the rainwater and the sand, e.g., olivine, wollastonite, etc. The reaction weathers the olivine, wollastonite, etc., and converts the carbonic acid into bicarbonate or carbonate. In this regard, carbonate and bicarbonate tend to be in equilibrium in aqueous solutions caused by weathering reactions because the dissolution of carbon dioxide and minerals generates a dynamic balance governed by pH-dependent acid-base reactions.\|[0038] By converting the carbon dioxide into other substances, the carbon dioxide can no longer be released into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These bicarbonate or carbonate solutions are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments, as well as integrated into marine animal carbonaceous mineral materials. These carbonate sediments form a sink for carbon dioxide.\|[0039] An example implementation of the embodiment described above is shown in FIG. 1. In this regard, FIG. 1 depicts a portion of a synthetic turf system 100 including carbon sequestration sand 102 that may be olivine-based, wollastonite-based, etc. and is utilized in one or more layers of infill materials. In accordance with some embodiments, the carbon sequestration sand 102 may be deposited in a layer having a thickness of about 1/16 to about ¼ inches, and have a particle size of about #4 mesh to about #270 mesh in the U.S. Standard Sieve Series. As will be appreciated, mesh may be defined as the number of openings in one square inch of a screen. A large mesh number means the pores in the screen are small. Sand's mesh size is determined by graining, and the numbers refer to the maximum and minimum grain diameters. 40/80 sand means that 90 percent of the sand by volume is small enough to pass through a #40 mesh screen, but too large to pass through an #80 mesh screen. As such, the range of particle size of the carbon sequestration sand 102 referenced in FIG. 1 may be about #4 mesh (4,750 μm) to about #270 mesh (53 μm).\|[0040] As shown in FIG. 1, the portion of the synthetic turf system 100 includes one or more infill layers 104 (described below), a permeable (e.g., carpet) backing 110, and turf fibers 112 that are artificial grass blades extended substantially perpendicular to the backing 110. With this construction, when the backing 110 is extended flatly in a horizontal direction, such as a stone base layer described in greater detail below, the turf fibers 112 may extend upward in a vertical direction perpendicular to the horizontal direction. While, as depicted, the turf fibers 112 are artificial grass blades, the turf fibers 112 may additionally or alternatively include natural grass blades extended upward from the backing 110, through the carbon sequestration sand 102 and the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0041] The infill layers 104 are positioned above the backing 110, in between the turf fibers 112, and below a top portion 114 of the turf fibers 112. More specifically, the infill layers 104 are disposed directly on top of the backing 110, where the top portion 114 of the turf fibers 112 extends above the infill layers 104. While, as depicted, the example embodiment of FIG. 1 includes multiple layers of infill materials respectively shown as a first layer 120, a second layer 122, and a third layer 124, the synthetic turf system 100 may include more or fewer distinct infill layers. Also, while, as depicted, the carbon sequestration sand 102 is disposed below the third layer 124 and directly contacts the backing 110, where the carbon sequestration sand 102 is interposed between and separates the infill layers 104 from the backing 110, the carbon sequestration sand 102 may additionally or alternatively be incorporated into the first layer 120, the second layer 122, or the third layer 124, or be applied over the third layer 124 as a top dressing of the synthetic turf system 100 without departing from the scope of the present disclosure.\|[0042] In this regard, the carbon sequestration sand 102 may partially or entirely form the first layer 120, the second layer 122, or the third layer 124 with a variety of compositional ranges. In an embodiment, the carbon sequestration sand 102 forms up to 90 percent of the first layer 120, the second layer 122, or the third layer 124 by volume. In a further embodiment, the carbon sequestration sand 102 forms up to 10 percent of the first layer 120, the second layer 122, or the third layer 124 by volume. With this construction, water insoluble components of the first layer 120, the second layer 122, or the third layer 124 reduce an overall wear rate of the synthetic turf system 100, and maintain a minimum volume in the synthetic turf system 100. In this manner, a wear rate and minimum volume of the first layer 120, the second layer 122, or the third layer 124 may be adjusted as desired by adjusting the compositional range of the carbon sequestration sand 102. In an embodiment, the carbon sequestration sand 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0043] The weathering rate and shape of particles forming the carbon sequestration sand 102 are influenced by material selection and particle size distribution. In this regard, consistent particle sizing promotes uniform weathering rates across the one or more infill layers 104, maintaining overall field performance and carbon sequestration efficiency in the synthetic turf system 100. The carbon sequestration sand 102 is accessible to rainwater traveling downward by gravity from the top portion 114 of the turf fibers 112 toward the backing 110. As the carbon sequestration sand 102 weathers through exposure to rainwater, its constituent particles may substantially change morphology, or alternatively may remain largely the same shape. In embodiments, the selected silicate rock, ultramafic rock, or reactive rock materials form weathered particles that maintain a sphericity of about 0.65 to about 0.85. This sphericity range supports stable packing within the synthetic turf system, reduces compaction variability, and ensures continued mechanical performance while facilitating consistent chemical reactions for carbon capture.\|[0044] In an embodiment where the carbon sequestration sand 102 is incorporated in the synthetic turf system 100 as a top dressing, the carbon sequestration sand 102 is periodically dispersed over the top portion 114 of the turf fibers 112 with an application system 130 depicted in FIG. 2. With continued reference to FIG. 2, the application system 130 includes a seed tender 132 and a tractor 134 that disperses the carbon sequestration sand 102 over the synthetic turf system 100 from a broadcaster tool 140. The seed tender 132 is employed in conjunction with a hydraulically-controlled conveyor 142 and a hopper gate 144, which supply the tractor 134 the carbon sequestration sand 102. As the tractor 134 moves at a consistent speed across the synthetic turf system 100 following a predetermined pattern, the hydraulically-controlled conveyor 142 and the hopper gate 144 precisely control a flow rate of the carbon sequestration sand 102 to the tractor 134, ensuring uniform distribution across the synthetic turf system 100.\|[0045] While, as depicted, the application system 130 includes the broadcaster tool 140 pulled by the tractor 134, and continuously fed the carbon sequestration sand 102 by the seed tender 132 along or across the synthetic turf system 100, the application system 130 may additionally or alternatively include a variety of components configured to spread granular material across a field, such as, for example, a self-propelled, manually powered, or power take-off (PTO) driven broadcast material spreader, a pneumatic spreader, an air boom spreader, a drop spreader, a handheld spreader, or an aerial spreader for dispersing the carbon sequestration sand 102 without departing from the scope of the present disclosure.\|[0046] Once the carbon sequestration sand 102 is dispersed across the synthetic turf system 100 by the application system 130, the carbon sequestration sand 102 is brushed into the one or more infill layers 104, including the first layer 120, the second layer 122, and the third layer 124. In this regard, a brush 150 depicted in FIG. 3 grooms the carbon sequestration sand 102 into the one or more infill layers 104. Rotary brush action on the synthetic turf system 100 from the top portion 114 by the brush 150 effectively works the carbon sequestration sand 102 downward between the turf fibers 112, ensuring proper placement within the infill material forming the one or more infill layers 104, while maintaining structural integrity and performance characteristics of the synthetic turf system 100, including at the top portion 114 and the first layer 120.\|[0047] While, as depicted, the brush 150 is a motorized, walk-behind rotary brush apparatus, such as a Shindaiwa or Laymor brush system, the brush 150 may additionally or alternatively include various components for incorporating the carbon sequestration sand 102 into the one or more infill layers 104 such as, for example, a ride-on turf groomer, a tractor-mounted brush that is dragged or PTO driven, or manual turf brushing equipment. Furthermore, brushes employed in such configurations may embody various shapes, sizes, and types, such as, for example, straight brushes, triangular brushes, hydraulic brushes, oscillating brushes, rigid brushes, flexible brushes, or brush assemblies including at least one plurality of brushes. Furthermore, the brush 150 may additionally or alternatively include specialty turf equipment, such as a vacuum or other devices complementary to the brush 150, and utilized to integrate the carbon sequestration sand 102 into the existing infill material of the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0048] Referring back to FIG. 1, infill is representative of material that is deposited over the backing 110 and forms the one or more infill layers 104 around the turf fibers 112. Infill is interspersed between the turf fibers 112 rising out of the backing 110. Infill generally has a depth that covers a portion of the turf fibers 112 (unexposed portion of the artificial fibers/blades) leaving part of the turf fibers 112, i.e., the top portion 114 extending above the infill (exposed portion of the artificial fibers/blades).\|[0049] In accordance with some embodiments, the one or more infill layers 104 assists in supporting the turf fibers 112 in an upright position and is used to provide traction and shock absorption. As a general matter, various types of infill arrangements are contemplated. For example, two layer, three layers, or other arrangements are contemplated. For convenience, the present description primarily discusses two and three layer embodiments.\|[0050] In some embodiments, the first layer 120 may include, for example and without limitation, heartwood or sapwood portions of hardwood or softwood, such as bamboo, cypress, poplar, pine, and cedar. The first layer 120 may additionally or alternatively include, for example and without limitation, cork, corn cobs, olive pits, barks, coconut peat or other organic materials, as well as styrene-butadiene rubber (SBR) particles ethylene propylene diene monomer (EPDM) rubber, other thermoplastics such as polyethylene, polypropylene, or composite materials can be used that combine thermoplastics, elastomers, reinforcements and/or fillers or other sufficient material. In accordance with some embodiments, the second layer 122 of infill material depicted in FIG. 1 may include a mixture of materials, e.g., material of the first layer 120 and a sand material. In such embodiments, the third layer 124 of infill material may include the aforementioned sand material, such that the fourth or lowermost layer is that of the carbon sequestration sand 102.\|[0051] In accordance with some embodiments, a shock pad (not shown) may be employed to achieve a desired shock absorption in accordance with a particular installation/purpose. For example, a shock pad (not shown) may be positioned below the one or more infill layers 104 shown in FIG. 1. As such, the material of the infill layers 104 conveys many of the mechanical properties that may be desired for use as artificial turf infill.\|[0052] In some embodiments, the carbon sequestration sand 102 can be used in combination with the backing 110, and/or a stabilizing infill layer (e.g., sand) 104 to make up the synthetic turf system 100. The synthetic turf system 100, using the described infill material, exhibits superior mechanical performance, a greater mechanical durability, easy availability and mitigates or otherwise avoids issues of floating away when subjected to large amounts of water.\|[0053] In some other embodiments, the backing 110 may be positioned below the carbon sequestration sand 102 shown in FIG. 1. In such embodiments, the backing 110 may correspond to the material into which the turf fibers 112 are woven, held, inserted, etc. Accordingly, the carbon sequestration sand 102 is positioned directly on the backing 110, thereby functioning as a ballast layer. The backing 110 is water permeable, without punched holes, such that the carbon sequestration sand 102 may remain in place at the backing 110, underlying the remainder of the infill layers 104, thereby maximizing contact with rainwater while preventing the carbon sequestration sand 102 from being flushed out of the synthetic turf system 100 via regular drainage measures. More specifically, the backing 110 has a porosity that filters rainwater from the carbon sequestration sand 102 and the one or more infill layers 104 as the rainwater travels downward through the synthetic turf system 100 from the one or more infill layers 104 to below the backing 110.\|[0054] Turning now to FIG. 4, there is shown a more detailed three-dimensional cross-sectional view of a portion of the synthetic turf system 100 utilizing the carbon sequestration sand 102 as a ballast infill material in accordance with the embodiment set forth above in FIG. 1. It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|[0055] As shown in FIG. 4, the synthetic turf system 100, in addition to including the turf fibers 112, the carbon sequestration sand 102, the infill layers 104, and the backing 110, further includes a first base stone layer 200 disposed below the backing 110 and above a second base stone layer 202. The synthetic turf system 100 further includes a geotextile component 204 that is a fabric disposed between the second base stone layer 202 and a subgrade 210. The synthetic turf system 100 may further include a subdrain trench component 212 formed in the subgrade and housing a drainage pipe 214.\|[0056] As discussed above, the carbon sequestration sand 102 may be implemented, for example and without limitation, olivine, wollastonite, basalt, limestone, etc. In operation, with reference to FIGS. 1 and 4, as rainwater contacts the carbon sequestration sand 102, a chemical reaction occurs between carbonic acid naturally present in the rainwater and the sequestration sand. The reaction weathers the carbon sequestration sand 102, e.g., olivine, wollastonite, etc., and converts the carbonic acid into carbonate or bicarbonate. As stated above, the conversion of the carbon dioxide into other substances prevents the release of the carbon dioxide into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. Carbonate and bicarbonate solutions may permeate the first base stone layer 200 and the second base stone layer 202, through the geotextile component 204 and into the subdrain trench component 212 and drainage pipe 214. Thereafter, the carbonate and bicarbonate solutions are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments, forming a sink for carbon dioxide.\|[0057] Turning now to FIG. 5, there is shown another embodiment of the synthetic turf system 100 utilizing the carbon sequestration sand 102. As illustrated in FIG. 5, the carbon sequestration sand 102 is applied on a top surface of the first base stone layer 200, below the backing 110. Application may be made via a suitable top-dressing machine, such as the application system 130 depicted in FIG. 2. In the embodiment of FIG. 5, the carbon sequestration sand 102 may be deposited with a thickness in the range of about 1/16″ to ¼″. The carbon sequestration sand 102 of FIG. 5 may be implemented with a particle size of about #4 mesh to #270 mesh. In such an embodiment, rainwater would flow directly through the one or more infill layers 104, the backing 110, and the carbon sequestration sand 102 and into the first base stone layer 200. Reaction with the rainwater would occur as described above with respect to FIGS. 1 and 4.\|[0058] With reference now to FIG. 6, there is illustrated the synthetic turf system 100 utilizing particles of the carbon sequestration sand 102 in accordance with another embodiment. In the embodiment depicted in FIG. 6, particles of the carbon sequestration sand 102 are incorporated into the first base stone layer 200. In accordance with one non-limiting example, the first base stone layer 200 may be implemented as a layer of stone having a thickness in the range of about 1 inch to about 6 inches, and in some particular embodiments, in the range of about 1 inch to about 2 inches. In such embodiments, the first base stone layer 200 may include for example and without limitation, a suitable drainage stone, such as gravel (e.g., granite) or the like. The carbon sequestration sand 102 may be suitably mixed with the stone to distribute the carbon sequestration sand 102 throughout the first base stone layer 200. In some embodiments, a single, e.g., uniform, base stone layer (not shown) may be utilized. In such embodiments, the carbon sequestration sand 102 may be blended into the single base stone layer, e.g., to a certain depth thereof (e.g., the top 1″ or 2″ thereof), or throughout the base stone layer. As described in greater detail above, reaction of the carbon sequestration sand 102 with rainwater would occur as described above with respect to FIGS. 1, 4, and 5.\|[0059] Turning now to FIG. 7, there is shown another embodiment of the synthetic turf system 100 utilizing carbon sequestration sand 102. As illustrated in FIG. 7, the carbon sequestration sand 102 may be on the geotextile component 204. In such a position, the carbon sequestration sand 102 may form a layer having a thickness of about 1/16″ to about ¼″, with a mesh size in the range of about #4 to about #270. Stated another way, the layer of carbon sequestration sand 102 may be applied at a bottom of the second base stone layer 202, as shown in FIG. 7. In accordance with one non-limiting example, the second base stone layer 202 may be implemented as a layer of stone having a thickness in the range of about 2 inches to about 6 inches, and in some particular embodiments, in the range of about 3 inches to about 4 inches. In such embodiments, the second base stone layer 202 may include, for example and without limitation, a suitable drainage stone, such as gravel (e.g., granite) or the like.\|[0060] In an embodiment, the first base stone layer 200 or the second base stone layer 202 includes silicate rocks, ultramafic rocks, or otherwise reactive rocks such as, for example, basalt, peridotite, olivine, dunite, limestone, and dolostone. Notably, in such an embodiment, the first base stone layer 200 or the second base stone layer 202 may perform carbon sequestration upon weathering by rainwater, in addition to the carbon sequestration sand 102, increasing an overall carbon sequestration capacity of the synthetic turf system 100.\|[0061] Although not shown, it is contemplated that the carbon sequestration sand 102 may be blended with the stone of the second base stone layer 202 similar to the manner described above with respect to FIG. 6. Similarly, although not illustrated in the accompanying figures, it is further contemplated that the carbon sequestration sand 102 may be blended with the stone of the subdrain trench component 212, or layered in the subdrain trench component 212 without blending. The above described positions of the carbon sequestration sand 102 would also enable the carbon capture reaction described above with respect to FIGS. 1 and 4-6.\|[0062] Referring now to FIG. 8, there is shown the synthetic turf system 100 utilizing the carbon sequestration sand 102 in accordance with another embodiment. As illustrated in FIG. 8, the carbon sequestration sand 102 may be tilled and incorporated into the subgrade 210 of the synthetic turf system 100, e.g., soil, sediment, etc. In such an implementation, the geotextile component 204 layered over the subgrade 210, and a 6″ to 8″ combined thickness of the first base stone layer 200 and the second base stone layer 202 may be installed on the subgrade 210 with the carbon sequestration sand 102 distributed therein. It will be appreciated that more carbon sequestration sand 102 may be used with this embodiment than the embodiments described above, thereby providing the synthetic turf system 100 additional carbon sequestration capability.\|[0063] Furthermore, it will be appreciated that by placing the carbon sequestration sand 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air. That is, as organic matter breaks down it creates additional carbon dioxide. As such, having the carbon sequestration sand 102 in the subgrade 210 where there is potential for more water availability increases the ability for the weathering reaction to occur, thereby facilitating carbon sequestration. In addition, as described above with respect to FIGS. 1 and 4-7, rainwater reaction with the carbon sequestration sand 102 provides the aforementioned carbon capture benefits.\|[0064] Referring to FIG. 9, a method 300 for preparing a synthetic turf system will be described according to an exemplary embodiment. FIG. 9 will be described with reference to FIGS. 1-8. For simplicity, the method 300 will be described as a sequence of blocks, but the elements of the method 300 can be organized into different architectures, elements, stages, and/or processes.\|[0065] At block 302, the method 300 includes measuring an aspect of the synthetic turf system 100. More specifically, a user may measure a thickness of an infill layer, such as one of the infill layers 104, may measure an acidity of rainwater at the infill layer, and may measure a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer.\|[0066] At block 304, the method 300 includes preblending or layering the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112. In an embodiment, the method 300 includes determining desired compositional ranges of the carbon sequestration sand 102 based on the measurement or measurements taken at block 302. In this manner, the wear rate and the minimum volume of the one or more infill layers 104 is controlled by adjusting the compositional ranges of components of the carbon sequestration sand 102. In an embodiment, the carbon sequestration sand 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0067] At block 310, the method 300 includes dispersing the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112, where the carbon sequestration sand 102 includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through the one or more infill layers 104 by gravity. In an embodiment, dispersing the carbon sequestration sand 102 includes dispersing a predetermined quantity of the carbon sequestration sand 102 over the top portion 114 of the turf fibers 112 as a top dressing based on the measurement taken at block 302.\|[0068] At block 312, the method 300 includes grooming the carbon sequestration sand 102 into the one or more infill layers 104 of the synthetic turf system 100, between the turf fibers 112, at the backing 110 of the synthetic turf system 100. In this regard, the brush 150 grooms the carbon sequestration sand 102 into and through the one or more infill layers 104, where the carbon sequestration sand 102 contacts and rests on the backing 110.\|[0069] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions and/or alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc., do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.\|[0070] While specific embodiments are shown and described herein, it is contemplated that alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc. without departing from the spirit and/or scope of the innovation as described in detail. These alternative embodiments are to be included within the spirit and scope of the innovation as described and claimed herein.\|[0071] Although the subject matter has been described in language specific to structural features or methodological acts, it is to be understood that the subject matter of the appended claims is not necessarily limited to the specific features or acts described above. Rather, the specific features and acts described above are disclosed as example aspects.\|[0072] Various operations of aspects are provided herein. The order in which one or more or all of the operations are described should not be construed as to imply that these operations are necessarily order dependent. Alternative ordering will be appreciated based on this description. Further, not all operations may necessarily be present in each aspect provided herein.\|[0073] As used in this application, “or” is intended to mean an inclusive “or” rather than an exclusive “or”. Further, an inclusive “or” may include any combination thereof (e.g., A, B, or any combination thereof). In addition, “a” and “an” as used in this application are generally construed to mean “one or more” unless specified otherwise or clear from context to be directed to a singular form. Additionally, at least one of A and B and/or the like generally means A or B or both A and B. Further, to the extent that “includes”, “having”, “has”, “with”, or variants thereof are used in either the detailed description or the claims, such terms are intended to be inclusive in a manner similar to the term “comprising”.\|[0074] Further, unless specified otherwise, “first”, “second”, or the like are not intended to imply a temporal aspect, a spatial aspect, an ordering, etc. Rather, such terms are merely used as identifiers, names, etc. for features, elements, items, etc. For example, a first channel and a second channel generally correspond to channel A and channel B or two different or two identical channels or the same channel. Additionally, “comprising”, “comprises”, “including”, “includes”, or the like generally means comprising or including, but not limited thereto.\|[0075] Further, the term “in” as used to describe an object with respect to a given direction (e.g., an edge extended in a left-right direction) is intended to denote an orientation that is substantially parallel to the specified direction. In contrast, the term “along” as used to describe an object with respect to a given direction (e.g., an edge extended along a vertical direction) is intended to indicate that a feature or element possesses a common vector component in that direction, even if its overall alignment is not strictly parallel.\|[0076] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.	Family Number\|(116035972)\|116035972\|Object of Invention\|(US20250297409 A1)\|According to another aspect, infill for a synthetic turf system includes carbon sequestration sand.\|In accordance with varying embodiments discussed herein, there is provided an artificial turf system that utilizes a material derived from one or more types of carbon sequestration sands, including, for example and without limitation, wollastonite sand (general formula CaSiO_3), limestone, basalt, or the like.\|(WO2025199637 A1)\|According to another aspect, a method of preparing a synthetic turf system includes dispersing carbon sequestration sand over a top portion of turf fibers, where the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a bicarbonate or carbonate with rainwater traveling through infill.\|According to another aspect, infill for a synthetic turf system includes carbon sequestration sand.\|In yet another aspect, a layer of carbon sequestration sand may be positioned on a geotextile or subgrade layer.\|Abstract\|(US20250297409 A1)\|A synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|(WO2025199637 A1)\|A synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|Title\|(US20250297409 A1)\|Carbon sequestration sand-based material for synthetic turf\|Carbon sequestration sand-based material for synthetic turf fields\|(WO2025199637 A1)\|Carbon sequestration sand-based material for synthetic turf\|Advantages / Prev. Drawbacks\|(US20250297409 A1)\|Furthermore, it will be appreciated that by placing the carbon sequestration sand 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air.\|It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|(WO2025199637 A1)\|It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the carbon sequestration sand 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1 -8 are intended solely as one non-limiting example of turf carpet systems in which the carbon sequestration sand 102 may be utilized.\|Independent Claims\|(US20250297409 A1)\| (...) wherein the one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\| (...) carbon sequestration sand including silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about #4 mesh to about #270 mesh; and organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\| (...) dispersing carbon sequestration sand over a top portion of turf fibers, wherein the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|(WO2025199637 A1)\|1. A synthetic turf system comprising: a backing; turf fibers extended upward from the backing; one or more infill layers positioned above the backing, below a top portion of the turf fibers; wherein the one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.\|12. Infill for a synthetic turf system, the infill comprising: carbon sequestration sand including silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, and has a particle size of about (...) particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the carbon sequestration sand.\|17. A method of preparing a synthetic turf system, the method comprising: dispersing carbon sequestration sand over a top portion of turf fibers, wherein the carbon sequestration sand includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|	Chemical engineering\|Civil engineering\|Environmental technology\|Textile and paper machines	D02G-003/44/5\|D10B-2403/02421\|D10B-2505/202\|E01C-013/02\|E01C-013/08		D02G-003/44/5\|D10B-2403/02421\|D10B-2505/202\|E01C-013/02\|E01C-013/08	B01D-053/02\|B01D-053/62\|B01J-020/10\|D02G-003/44\|E01C-013/08	B01D-053/02\|B01D-053/62\|B01J-020/10\|D02G-003/44\|E01C-013/08					WO2020142232\|WO2021204310\|US20220049450	WO2020142232 89636781 WHO=Examiner SELF=N CAT=X CAT=Y CAT=A\|WO2021204310 96459586 WHO=Examiner SELF=N CAT=X CAT=Y\|US20220049450 98730333 WHO=Examiner SELF=N CAT=X CAT=A		WO2021204310; WO2020142232; US20220049450\|		PENDING	(US20250297409)\|PENDING\|(WO2025/199637)\|PENDING	ALIVE	(US20250297409)\|ALIVE\|(WO2025/199637)\|ALIVE	(US20250297409)\|LEGAL DETAILS FOR US20250297409\|Actual or expected expiration date=2045-03-25\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-03-25\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19089278\|Application date=2025-03-25\|Standardized application number=2025US-19089278\|Event publication date=2025-03-25\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-03-25\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-03-25\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 58213-00345\|Event publication date=2025-03-25\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 136458\|Event publication date=2025-03-25\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2025-03-25\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-03-25\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2025-03-25\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-03-25\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-03-31\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:SMOLETT, JASON;HABIB, ERIC;CHISAM, CHRISTOPHER;SIGNING DATES FROM 20250320 TO 20250326\|Reel/frame:070683/0386\|OWNER:TARKETT SPORTS CANADA INC., CANADA\|Event publication date=2025-04-01\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-04-28\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-04-28\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-07-15\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2025-09-25\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250297409\|Publication stage code=A1\|Publication date=2025-09-25\|Standardized publication number=US20250297409\|Event publication date=2025-09-25\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|(WO2025/199637)\|LEGAL DETAILS FOR WO2025/199637\|Actual or expected expiration date=2027-09-25\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-03-25\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOCA2025/050423\|Application date=2025-03-25\|Standardized application number=2025WO-CA50423\|Event publication date=2025-10-02\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/199637\|Publication stage code=A1\|Publication date=2025-10-02\|Standardized publication number=WO2025199637\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2045-03-25\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP25778857\|Event publication date=2025-11-12\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP	(WO2025/199637)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/199637)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/199637)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/199637)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/199637)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UY, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(US20250297409)\|US\|(WO2025/199637)\|WO; EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcP1jvMh5Li0oTkuDREcUBY0JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023019215&ekey=1918&xpn=US20250297409&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19089278/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=zeXk%252BPpISmSlgNU07Y9GJ8RHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2025/199637)\|CA\|(US20250297409)\|CA	(WO2025/199637)\|NAME=TARKETT SPORTS CANADA INC. 7445 Cote-de-Liesse Rd. Suite 200 Montreal, Québec H4T 1G2 , COUNTRY=CA\|(US20250297409)\|NAME=Tarkett Sports Canada Inc. , CITY=Montreal , COUNTRY=CA	(WO2025/199637)\|CA	(WO2025/199637)\|NAME=YIP, Vincent Suite 2400 745 Thurlow Street Vancouver, British Columbia V6E 0C5 , POSTCODE=V6E 0C5 , COUNTRY=CA	(US20250297409)\|CA; CA; US\|(WO2025/199637)\|CA; CA; US	(US20250297409)\|NAME=Smolett Jason, CITY=Kirkland, COUNTRY=CA \|NAME=Habib Eric, CITY=Pierrefonds, COUNTRY=CA \|NAME=Chisam Christopher, CITY=Granite Bay, STATE=CA , COUNTRY=US\|(WO2025/199637)\|NAME=SMOLETT, Jason 71 Rondeau Kirkland, Québec H9H 4J2, POSTCODE=H9H 4J2, COUNTRY=CA \|NAME=HABIB, Eric 4967 Saint Barnabas Pierrefonds, Québec H8Z 3B9, POSTCODE=H8Z 3B9, COUNTRY=CA \|NAME=CHISAM, Christopher 9792 Swan Lake Drive Granite Bay, California 95746, POSTCODE=95746, COUNTRY=US	(WO2025/199637)\|9\|(US20250297409)\|9	2	2					(US20250297409)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,12,17\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|\|(WO2025/199637)\|Number of Claims: NCL=20\|Extended kind: EXTK=x\|	(US20250297409)\|Provisional Appl: US63/569,558 FDD=2024-03-25 [2024US-63569558]	(US20250297409)\|ENGLISH (ENG)	(WO2025199637)\|Patent\|(US20250297409)\|Patent	Titre: (US20250297409)\|Carbon sequestration sand-based material for synthetic turf fields Résumé: (US20250297409)\|A synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes carbon sequestration sand, or the synthetic turf system further comprises a layer of carbon sequestration sand disposed above or below the one or more infill layers.	8	Abstract	gpt-4o-mini	no	The article focuses on a synthetic turf system that includes carbon sequestration sand, which does not relate to the accelerated weathering of minerals for CO₂ capture.
14	CN202411779739	CN202411779739	CN119666501	113895166	CN119666501 A 2025-03-21 [CN119666501]	2024-12-05	2024-12-05	2025-03-21		(CN119666501)\|2044-12-05	(CN119666501)\|Method for determining total organic carbon content in rock	(CN119666501)\|The invention discloses a method for determining the total organic carbon content in rock, which comprises the following steps: grinding a rock sample, and weighing a preset mass of crushed rock sample; putting the weighed crushed rock sample into a container, and adding an excessive hydrochloric acid solution into the container; washing the crushed rock sample treated by hydrochloric acid with distilled water until the crushed rock sample is neutral; picking the cleaned broken rock sample under a microscope; burning the broken rock sample with the elemental carbon removed in high-temperature oxygen flow, and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample. The method has the beneficial effects that after inorganic carbon in the sample is removed through diluted hydrochloric acid, the sample is picked under a microscope, simple substance carbon in the crushed rock sample is removed, then the crushed rock sample with the simple substance carbon removed is combusted in high-temperature oxygen flow, the total organic carbon is converted into carbon dioxide, the content of the total organic carbon is obtained through an infrared detector, and the content of the total organic carbon in the crushed rock sample is calculated. And the accuracy of the total organic carbon content determination result can be improved.	SHAANXI YANCHANG PETROLEUM	(CN119666501)\|SHAANXI YANCHANG PETROLEUM (GROUP) CO. LTD. ([CN])	LIU SHUANGSHUANG\|CUI PENGXING\|LIU LILI\|KANG SHENGSONG\|ZHAO XUESI\|WANG TAO\|ZHU TONGTONG	(CN119666501)\|LIU SHUANGSHUANG\|CUI PENGXING\|LIU LILI\|KANG SHENGSONG\|ZHAO XUESI\|WANG TAO\|ZHU TONGTONG	(CN119666501)\|HE SHAN;XIAN YINUO PATENT AGENT CO. LTD.\|Reg. Nb: 61220	(CN119666501)\|However, the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, for example, for the coal-bearing formation, the rock sample may contain elemental carbon such as graphite and amorphous carbon, and the elemental carbon is stable at normal temperature and does not react with the dilute hydrochloric acid, so that the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, which results in a higher content of the measured total organic carbon.\|	(CN119666501)\|1. A method for determining total organic carbon content in rock, comprising: s1, grinding a rock sample, and weighing rock fragments with preset mass; S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; S4, picking the cleaned crushed rock sample under a microscope, and removing simple substance carbon in the crushed rock sample; And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|	(CN119666501)\|The invention discloses a method for measuring total organic carbon content in rock, which comprises the steps of grinding a rock sample, weighing rock fragments with preset mass, placing the weighed rock fragments into a container, adding excessive hydrochloric acid solution into the container, washing the rock fragments subjected to hydrochloric acid treatment to be neutral through distilled water, picking the washed rock fragments under a microscope, burning the rock fragments subjected to simple substance carbon removal in high-temperature oxygen flow, and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample.\|The invention relates to the technical field of total organic carbon content measurement, in particular to a method for measuring total organic carbon content in rock.\|the invention provides a method for measuring the content of total organic carbon in rock, which comprises the following steps:\|	(CN119666501)\|TOTAL ORGANIC CARBON(100,55)\|TOTAL ORGANIC CARBON CONTENT(100,29)\|ROCK(100,28)\|WASHED ROCK FRAGMENT(100,1)\|ROCK SAMPLE(95,15)\|CRUSHED ROCK SAMPLE(84,23)\|WEIGHED ROCK(84,1)\|ELEMENTAL CARBON(72,15)\|MICROSCOPIC PICKING(62,7)\|TRANSPARENT PIPE(61,10)\|MICROSCOPE(58,22)\|WEIGHED CRUSHED ROCK(56,3)\|PRESET DEVICE MASS(53,4)\|CONTENT MEASUREMENT(51,4)\|CLEANED CRUSHED ROCK SAMPLE(50,3)\|BUFFER TANK(49,18)\|BURNER(49,18)\|GRAVEL(47,13)\|HYDROCHLORIC ACID(46,20)\|SUCKING SUBSTANCE CARBON(46,1)\|SUCKING ELEMENTAL CARBON PARTICLE(43,3)\|SUBSTANCE CARBON(42,13)\|SCREW HOLE(42,9)\|SUBSTANCE CARBON REMOVAL(42,4)\|ENTIRE INORGANIC CARBON(42,2)\|SLIDING SLEEVE(39,22)\|INFRARED DETECTOR(38,20)\|WEIGHED CRUSHED ROCK SAMPLE(38,2)\|INORGANIC CARBON(37,7)\|HYDROCHLORIC ACID TREATMENT(36,8)\|OUTPUT PIPE(35,10)\|CACHE TANK(33,2)\|OXYGEN STREAM(32,3)\|BLOCKING NET(32,2)\|HYDROCHLORIC ACID SOLUTION(31,4)\|GAS OUTLET(30,9)\|COAL BEARING FORMATION(30,1)\|HOLE INCLINATION(29,6)\|CONTENT DETECTION(28,7)\|IGNITER(28,7)\|COMBUSTION TABLE(27,6)\|GRAVEL PLACEMENT(27,3)\|OXYGEN FLOW(27,3)\|OXYGEN INLET(25,5)\|CLOSED COMBUSTION CAVITY(25,2)\|GENERATED CARBON DIOXIDE CONTENT(25,1)\|GENERATED CARBON DIOXIDE(24,5)\|CARBON DIOXIDE(22,17)\|GAS INLET(22,6)\|GAS EXHAUST PIPE(21,6)\|AIR INLET(19,6)\|DISTILLED WATER(19,5)\|GRAPHITE(19,4)\|CROSS ROD(18,8)\|THREADED CONNECTION(18,6)\|SUCTION PUMP(17,8)\|OXYGEN TANK(16,8)\|PLATE POSITION(16,2)\|OUTLET VALVE(15,13)\|AMORPHOUS CARBON(15,4)\|GAS GUIDE VALVE(15,3)\|PLACING PLATE(14,3)\|OUTPUT VALVE(13,5)\|GAS EXHAUST VALVE(13,3)\|OBJECTIVE LENS(13,3)\|WATER OUTLET(13,3)\|TUNGSTEN PARTICLE COSOLVENT(12,1)\|WEIGHED ROCK FRAGMENT MASS(12,1)\|AIR PUMP(11,10)\|EVALUATING ABUNDANCE(10,1)\|SCIENTIFIC APPARATUS PLATE(9,4)\|AUXILIARY PIPELINE(9,1)\|MONTANT BUTT(9,1)\|SCRAP IRON COSOLVENT(9,1)\|ADJUSTED POSITION(8,3)\|HORIZONTAL DIRECTION(8,3)\|PRESSURE DETECTING MEMBER(8,3)\|WATER BATH TEMPERATURE(7,3)\|OBJECT POSITION(7,2)\|ABSORBING SUBSTANCE CARBON(7,1)\|HORIZONTAL POLE BUTT(7,1)\|ROCK POWDER(7,1)\|SEALED COMBUSTION CAVITY(7,1)\|AIR OUTLET(6,3)\|	(CN119666501)\|1. A method for determining total organic carbon content in rock, comprising:\| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope, and removing simple substance carbon in the crushed rock sample; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|2. The method for measuring the content of total organic carbon in rock according to claim 1, wherein in the step S1, the mass of the weighed crushed rock sample is 0.01-1.00g.\|3. The method for measuring the total organic carbon content in rock according to claim 1, wherein in the step S2, the container is placed in a water bath, and the temperature of the water bath is controlled to be 60-80 ℃.\|4. The method according to claim 1, wherein in the step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by a sample washing device, the sample washing device comprises a cylinder and a screen, the upper end of the cylinder is provided with an opening, the lower end of the cylinder is provided with a water outlet, and the screen is detachably mounted at the opening of the upper end of the cylinder.\|5. The method according to claim 1, wherein in the step S4, the cleaned crushed rock is picked by a microscopic picking device, so as to remove the elemental carbon in the crushed rock, the microscopic picking device comprises a base, a placing plate, a microscope, a position adjusting mechanism and a picking mechanism, the microscope is located above the base, the placing plate is used for placing the crushed rock on the base, the position adjusting mechanism is connected with the microscope and used for adjusting the position of an objective lens of the microscope, and the picking mechanism is used for sucking the elemental carbon particles.\|6. The method for measuring the total organic carbon content in rock according to claim 5, wherein the position adjusting mechanism comprises a vertical rod, a vertical sliding sleeve, a vertical screw, a transverse sliding sleeve, a cross rod, a transverse screw and a bracket, wherein the lower end of the vertical rod is fixed on the base, the vertical sliding sleeve is slidably sleeved on the vertical rod and extends along the vertical direction, a first screw hole is formed in the vertical sliding sleeve, the vertical screw is in threaded connection with the first screw hole and is used for being abutted to the vertical rod, the transverse sliding sleeve is fixed on the vertical sliding sleeve and extends along the horizontal direction, the cross rod is slidably inserted in the transverse sliding sleeve, a second screw hole is formed in the transverse sliding sleeve, the transverse screw is in threaded connection with the second screw hole and is used for being abutted to the cross rod, the bracket is fixed on one end of the cross rod, and the bracket is fixedly connected with a microscope.\|7. The method for measuring the total organic carbon content in rock according to claim 6, wherein the bracket is provided with an inclined hole which is obliquely arranged, the sampling mechanism comprises a transparent pipe, a blocking net, a suction pump and a connecting hose, the transparent pipe is slidably inserted into the inclined hole, the lower end of the transparent pipe is used for sucking the simple substance carbon on the object placing plate, the blocking net is fixed at the lower end of the transparent pipe, and the inlet of the suction pump is communicated with the upper end of the transparent pipe through the connecting hose.\|8. The method for determining the total organic carbon content in rock according to claim 1, wherein in the step S4, the crushed rock sample from which the elemental carbon is removed is burned in a high-temperature oxygen stream by a total organic carbon content detection device, and the content of carbon dioxide generated is detected by an infrared detector, so as to obtain the total organic carbon content of the rock sample, and the total organic carbon content detection device comprises a burner, an oxygen introducing mechanism, a buffer mechanism and the infrared detector;\| The burner comprises a burner body, a combustion table and an igniter, wherein a closed combustion cavity is formed in the burner body, an air inlet communicated with the combustion cavity is formed in one end of the burner body, an air outlet communicated with the combustion cavity is formed in the other end of the burner body, the combustion table is arranged in the burner body, and the igniter is arranged in the burner body; \| the oxygen inlet mechanism comprises an oxygen tank, an outlet valve, an air pump and an output pipe, the outlet valve is arranged at the outlet of the oxygen tank, the inlet of the air pump is communicated with the outlet valve, the outlet of the air pump is communicated with one end of the output pipe, the other end of the output pipe is communicated with the air inlet, and the output pipe is provided with the output valve; \| The buffer mechanism comprises a buffer tank and a vacuum pump, wherein a gas inlet is formed in one end of the buffer tank, a gas outlet is formed in the other end of the buffer tank, the gas inlet is communicated with the gas outlet through a conduit, a gas guide valve is arranged on the conduit, the inlet of the vacuum pump is communicated with the gas outlet through a gas exhaust pipe, and the gas exhaust pipe is provided with a gas exhaust valve; \| The infrared detector is arranged in the cache tank. \|9. The method for measuring the total organic carbon content in rock according to claim 8, wherein a one-way valve is further arranged on the output pipe.\|10. The method for measuring the total organic carbon content in rock according to claim 8, wherein a pressure detecting member is provided on the buffer tank.	(CN119666501)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of total organic carbon content measurement, in particular to a method for measuring total organic carbon content in rock.\|BACKGROUND ART\|[0002] The total organic carbon content (TOC) in rock refers to the mass of organic carbon per mass of rock, typically expressed as mass fraction (%). The index has important significance in geology and oil and gas exploration, and is commonly used for evaluating the abundance, maturity and hydrocarbon production potential of organic matters of hydrocarbon source rocks.\|[0003] The existing method for measuring the content of the total organic carbon in the rock is to remove inorganic carbon in a sample by using dilute hydrochloric acid, burn the inorganic carbon in high-temperature oxygen flow, convert the total organic carbon into carbon dioxide, and send the content of the total organic carbon through an infrared detector.\|[0004] However, the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, for example, for the coal-bearing formation, the rock sample may contain elemental carbon such as graphite and amorphous carbon, and the elemental carbon is stable at normal temperature and does not react with the dilute hydrochloric acid, so that the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, which results in a higher content of the measured total organic carbon.\|DISCLOSURE\|Disclosure of Invention\|[0005] The invention aims to overcome the technical defects, and provides a method for measuring the total organic carbon content in rock, which solves the technical problem that the content of the measured total organic carbon is higher because simple substance carbon such as graphite, amorphous carbon and the like possibly contained in a rock sample is not removed in the method for measuring the total organic carbon content in the prior art.\|[0006] In order to achieve the technical purpose, the invention adopts the following technical scheme:\| the invention provides a method for measuring the content of total organic carbon in rock, which comprises the following steps: \| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope, and removing simple substance carbon in the crushed rock sample; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|[0007] In some embodiments, in step S1, the mass of the weighed rock fragments is 0.01-1.00g.\|[0008] In some embodiments, in step S2, the container is placed in a water bath, and the temperature of the water bath is controlled to be 60-80 ℃.\|[0009] In some embodiments, in step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by a sample washing device, where the sample washing device includes a cylinder and a screen, an opening at an upper end of the cylinder is provided, a water outlet is provided at a lower end of the cylinder, and the screen is detachably mounted at the opening at the upper end of the cylinder.\|[0010] In some embodiments, in step S4, the cleaned crushed rock is picked by a microscopic picking device, so as to remove elemental carbon in the crushed rock, where the microscopic picking device includes a base, a placing plate, a microscope, a position adjusting mechanism and a picking mechanism, the microscope is located above the base, the placing plate is used for placing the crushed rock on the base, the position adjusting mechanism is connected with the microscope and used for adjusting the position of an objective lens of the microscope, and the picking mechanism is used for sucking elemental carbon particles.\|[0011] In some embodiments, the position adjustment mechanism includes montant, vertical sliding sleeve, vertical screw, horizontal sliding sleeve, horizontal pole, horizontal screw and support, the lower extreme of montant is fixed in the base, vertical sliding sleeve locates the montant to extend along vertical direction, set up first screw on the vertical sliding sleeve, vertical screw threaded connection in first screw, and be used for with montant butt, horizontal sliding sleeve is fixed in vertical sliding sleeve to extend along the horizontal direction, the horizontal pole slides and inserts and locate in the horizontal sliding sleeve, the second screw has been seted up on the horizontal sliding sleeve, horizontal screw threaded connection in the second screw, and be used for with the horizontal pole butt, the support is fixed in the one end of horizontal pole, the support with microscope fixed connection.\|[0012] In some embodiments, the support is provided with an inclined hole arranged obliquely, the sampling mechanism comprises a transparent pipe, a blocking net, a suction pump and a connecting hose, the transparent pipe is slidably inserted into the inclined hole, the lower end of the transparent pipe is used for absorbing simple substance carbon on the object placing plate, the blocking net is fixed at the lower end of the transparent pipe, and an inlet of the suction pump is communicated with the upper end of the transparent pipe through the connecting hose.\|[0013] In some embodiments, in the step S4, the crushed rock sample after removing the elemental carbon is burned in a high-temperature oxygen stream by a total organic carbon content detection device, and the content of the generated carbon dioxide is detected by an infrared detector, so as to obtain the total organic carbon content of the rock sample, where the total organic carbon content detection device includes a burner, an oxygen inlet mechanism, a buffer mechanism and the infrared detector;\| The burner comprises a burner body, a combustion table and an igniter, wherein a closed combustion cavity is formed in the burner body, an air inlet communicated with the combustion cavity is formed in one end of the burner body, an air outlet communicated with the combustion cavity is formed in the other end of the burner body, the combustion table is arranged in the burner body, and the igniter is arranged in the burner body; \| the oxygen inlet mechanism comprises an oxygen tank, an outlet valve, an air pump and an output pipe, the outlet valve is arranged at the outlet of the oxygen tank, the inlet of the air pump is communicated with the outlet valve, the outlet of the air pump is communicated with one end of the output pipe, the other end of the output pipe is communicated with the air inlet, and the output pipe is provided with the output valve; \| The buffer mechanism comprises a buffer tank and a vacuum pump, wherein a gas inlet is formed in one end of the buffer tank, a gas outlet is formed in the other end of the buffer tank, the gas inlet is communicated with the gas outlet through a conduit, a gas guide valve is arranged on the conduit, the inlet of the vacuum pump is communicated with the gas outlet through a gas exhaust pipe, and the gas exhaust pipe is provided with a gas exhaust valve; \| The infrared detector is arranged in the cache tank. \|[0014] In some embodiments, a one-way valve is also provided on the output tube.\|[0015] In some embodiments, the buffer tank is provided with a pressure detecting member thereon.\|[0016] Compared with the prior art, the method for measuring the total organic carbon content in the rock has the beneficial effects that: removing inorganic carbon in a sample through dilute hydrochloric acid, picking under a microscope to remove simple substance carbon in the crushed rock sample, burning the crushed rock sample after removing the simple substance carbon in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and obtaining the content of the total organic carbon through an infrared detector.\|DRAWINGS DESCRIPTION\|[0017] Fig. 1 is a schematic structural diagram of a method for measuring total organic carbon content in rock according to an embodiment of the present invention.\|[0018] Fig. 2 is a schematic structural view of the sample washing apparatus used in step S3 in fig. 1.\|[0019] Fig. 3 is a schematic structural diagram of a microscopic picking device used in step S4 in fig. 1.\|[0020] Fig. 4 is a partial enlarged view of the area a in fig. 3.\|[0021] FIG. 5 is a schematic view of the microscope sampling device of FIG. 3 when the transparent tube is lifted.\|[0022] Fig. 6 is a schematic view of the microscope sampling device of fig. 5 at another perspective.\|[0023] Fig. 7 is a schematic structural diagram of the total organic carbon content detecting device used in step S5 in fig. 1.\|[0024] The reference numerals are 100-sample cleaning device, 110-cylinder, 111-water outlet, 120-screen, 200-microscopic sample picking device, 210-base, 220-object placing plate, 230-microscope, 240-position adjusting mechanism, 241-vertical rod, 242-vertical sliding sleeve, 243-vertical screw, 244-horizontal sliding sleeve, 245-horizontal rod, 246-horizontal screw, 247-bracket, 250-sample picking mechanism, 251-transparent tube, 252-blocking net, 300-total organic carbon content detecting device, 310-burner, 311-furnace body, 312-combustion table, 313-igniter, 320-oxygen inlet mechanism, 321-oxygen tank, 322-outlet valve, 323-air pump, 324-output pipe, 325-output valve, 326-one-way valve, 330-buffering mechanism, 331-buffering tank, 3311-pressure detecting piece, 332-vacuum pump, 333-conduit, 334-air guide valve, 335-air suction tube, 336-suction valve, 340-infrared detector.\|INVENTION MODE\|Detailed Description\|[0025] The present invention will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0026] In order to solve the technical problem that the content of the measured total organic carbon is higher because simple substance carbon such as graphite and amorphous carbon possibly contained in a rock sample is not removed in the total organic carbon content measuring method, the invention provides the total organic carbon content measuring method in the rock, and the accuracy of measuring the total organic carbon content can be improved.\|[0027] Referring to fig. 1, fig. 1 is a flow chart of a method for determining total organic carbon content in rock according to an embodiment of the invention, the method for determining total organic carbon content in rock includes the following steps:\| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope to remove the simple substance carbon in the crushed rock sample, wherein the simple substance carbon in the rock is mainly graphite and amorphous carbon which are black, and the rock powder is usually light, so that the simple substance carbon can be easily identified and removed under the microscope; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|[0028] According to the technical scheme provided by the invention, after inorganic carbon in a sample is removed through dilute hydrochloric acid, sample picking is performed under a microscope to remove simple substance carbon in the rock fragments, then the rock fragments after simple substance carbon removal are combusted in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and the content of the total organic carbon is obtained through an infrared detector.\|[0029] In one embodiment, referring to fig. 1, in the step S1, the rock sample is ground to a particle size of less than 0.2mm, the mass of the ground sample is not less than 10g, and in the step S1, the mass of the weighed crushed rock sample is 0.01-1.00g, and is accurate to 0.0001g.\|[0030] In one embodiment, referring to fig.1, in the step S2, the container is placed in a water bath, the temperature of the water bath is controlled to be 60-80 ℃, and the sample is dissolved for more than 2 hours until the reaction is complete.\|[0031] In one embodiment, referring to fig. 1 and 2, in step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by the sample washing device 100, the sample washing device 100 includes a cylinder 110 and a screen 120, an upper end opening of the cylinder 110 is disposed, a water outlet 111 is disposed at a lower end of the cylinder 110, and the screen 120 is detachably mounted at the upper end opening of the cylinder 110. In use, the crushed rock sample after hydrochloric acid treatment is poured into the screen 120, and distilled water boiled is continuously introduced into the screen until the pH value of the crushed rock sample is neutral.\|[0032] In one embodiment, referring to fig. 1 and 3, in step S4, the cleaned crushed rock is picked by a microscopic picking device 200 to remove elemental carbon in the crushed rock, the microscopic picking device 200 includes a base 210, a placing plate 220, a microscope 230, a position adjusting mechanism 240, and a picking mechanism 250, the microscope 230 is located above the base 210, the placing plate 220 is used for placing the crushed rock on the base 210, the position adjusting mechanism 240 is connected with the microscope 230 and is used for adjusting the position of an objective lens of the microscope 230, and the picking mechanism 250 is used for sucking elemental carbon particles.\|[0033] In one embodiment, please refer to fig. 3-6, the position adjusting mechanism 240 includes a vertical rod 241, a vertical sliding sleeve 242, a vertical screw 243, a horizontal sliding sleeve 244, a cross rod 245, a horizontal screw 246 and a support 247, wherein the lower end of the vertical rod 241 is fixed in the base 210, the vertical sliding sleeve 242 is slidably sleeved on the vertical rod 241 and extends along the vertical direction, a first screw hole is formed in the vertical sliding sleeve 242, the vertical screw 243 is in threaded connection with the first screw hole and is used for being in butt joint with the vertical rod 241, the horizontal sliding sleeve 244 is fixed in the vertical sliding sleeve 242 and extends along the horizontal direction, the cross rod 245 is slidably inserted in the horizontal sliding sleeve 244, a second screw hole is formed in the horizontal sliding sleeve 244, the horizontal screw 246 is in threaded connection with the second screw hole and is used for being in butt joint with the cross rod 245, the support 247 is fixed at one end of the cross rod 245, the support 247 is fixedly connected with the microscope 230, and when in use, the vertical screw 243 is unscrewed, namely, the vertical sliding sleeve 242 is in threaded connection with the first screw hole, and is used for being in threaded connection with the vertical sliding sleeve 241, so as to enable the vertical sliding sleeve 241 to rotate around the microscope 241, thereby enable the vertical sliding sleeve 241 to rotate around the vertical rod 241, and the microscope 241 to reach the position of the microscope 230, and the position of the microscope 230 can be changed, and the position of the microscopic plate 220 can be different from the position of the microscopic plate 220, and the microscopic plate 220 can be in turn, or the position of the microscopic plate 220, and the position can be changed.\|[0034] In one embodiment, referring to fig. 3-6, the support 247 is provided with an inclined hole, the sample picking mechanism 250 includes a transparent tube 251, a blocking net 252, a suction pump (not shown) and a connection hose (not shown), the transparent tube 251 is slidably inserted into the inclined hole, the lower end of the transparent tube 251 is used for sucking the elemental carbon on the object placing plate 220, the blocking net 252 is fixed at the lower end of the transparent tube 251, the inlet of the suction pump is communicated with the upper end of the transparent tube 251 through the connection hose, when in use, the lower end of the transparent tube 251 is aligned with the elemental carbon, then the suction pump is started, the elemental carbon is sucked into the transparent tube 251 by the blocking net 252, then the transparent tube 251 is lifted, then the material receiving box is placed at the lower end of the transparent tube 251, then the suction pump is closed, and the elemental carbon in the transparent tube 251 falls into the material receiving box under the action of gravity, thereby removing the elemental carbon.\|[0035] In one embodiment, referring to fig. 1 and 7, in step S4, a crushed rock sample from which elemental carbon is removed is burned in a high-temperature oxygen stream by a total organic carbon content detection device 300, and the content of carbon dioxide generated is detected by an infrared detector to obtain the total organic carbon content of the rock sample, where the total organic carbon content detection device 300 includes a burner 310, an oxygen inlet mechanism 320, a buffer mechanism 330, and an infrared detector 340;\| the burner 310 comprises a burner body 311, a burner table 312 and an igniter 313, wherein a sealed combustion cavity is arranged in the burner body 311, an air inlet communicated with the combustion cavity is formed in one end of the burner body 311, an air outlet communicated with the combustion cavity is formed in the other end of the burner body 311, the burner table 312 is arranged in the burner body 311, and the igniter 313 is arranged in the burner body 311; \| The oxygen inlet mechanism 320 comprises an oxygen tank 321, an outlet valve 322, an air pump 323 and an output pipe 324, the outlet valve 322 is arranged at the outlet of the oxygen tank 321, the inlet of the air pump 323 is communicated with the outlet valve 322, the outlet of the air pump 323 is communicated with one end of the output pipe 324, the other end of the output pipe 324 is communicated with the air inlet, and the output pipe 324 is provided with an output valve 325; \| The buffer mechanism 330 comprises a buffer tank 331 and a vacuum pump 332, wherein a gas inlet is formed at one end of the buffer tank 331, a gas outlet is formed at the other end of the buffer tank 331, the gas inlet is communicated with the gas outlet through a conduit 333, a gas guide valve 334 is arranged on the conduit 333, an inlet of the vacuum pump 332 is communicated with the gas outlet through a gas exhaust pipe 335, and a gas exhaust valve 336 is arranged on the gas exhaust pipe 335; \| the infrared detector 340 is disposed in the buffer tank 331. \|[0036] The detection flow of the total organic carbon content detection device 300 is as follows:\| (1) Uniformly mixing the crushed rock sample after removing the simple substance carbon with the scrap iron cosolvent and the tungsten particle cosolvent, and placing the mixture in a combustion table 312; \| (2) Vacuumizing, closing the outlet valve 322, opening the output valve 325, the air guide valve 334 and the air extraction valve 336, and then opening the vacuum pump 332, wherein the vacuum pump vacuumizes the buffer tank 331, the oxygen tank 321 and the pipeline; \| (3) Oxygen is introduced, the air extraction valve 336 and the air guide valve 334 are closed, the outlet valve 322 is opened, and sufficient oxygen is introduced into the combustion chamber; \| (4) The igniter 313 ignites the sample on the combustion table 312, continuously introduces oxygen, and then opens the outlet valve 322 to introduce the generated gas into the buffer tank 331; \| (5) After full combustion, the output valve 325 is closed, combustion is stopped, after the system is stable, the carbon dioxide concentration in the buffer tank 331 is detected through the infrared detector 340, the carbon dioxide concentration in the buffer tank 331 is equal to the carbon dioxide concentration in the furnace body 311, the total amount of carbon dioxide generated by combustion can be obtained according to the carbon dioxide concentration multiplied by the total volume of the buffer tank 331, the furnace body 311 and the auxiliary pipeline, the total amount of organic carbon in the crushed rock sample is further obtained, and the total organic carbon content in the crushed rock sample can be obtained by dividing the total amount by the mass of the crushed rock sample. \|[0037] In one embodiment, referring to fig. 1 and 7, the output pipe 324 is further provided with a check valve 326, so as to avoid reverse flow of the gas.\|[0038] In one embodiment, referring to fig. 1 and 7, a pressure detecting member 3311 is provided on the buffer tank 331 to facilitate control of the reaction pressure.\|[0039] According to the technical scheme provided by the invention, after inorganic carbon in a sample is removed through dilute hydrochloric acid, sample picking is performed under a microscope to remove simple substance carbon in the rock fragments, then the rock fragments after simple substance carbon removal are combusted in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and the content of the total organic carbon is obtained through an infrared detector.\|[0040] The above-described embodiments of the present invention do not limit the scope of the present invention. Any other corresponding changes and modifications made in accordance with the technical idea of the present invention shall be included in the scope of the claims of the present invention.	(CN119666501)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of total organic carbon content measurement, in particular to a method for measuring total organic carbon content in rock.\|BACKGROUND ART\|[0002] The total organic carbon content (TOC) in rock refers to the mass of organic carbon per mass of rock, typically expressed as mass fraction (%). The index has important significance in geology and oil and gas exploration, and is commonly used for evaluating the abundance, maturity and hydrocarbon production potential of organic matters of hydrocarbon source rocks.\|[0003] The existing method for measuring the content of the total organic carbon in the rock is to remove inorganic carbon in a sample by using dilute hydrochloric acid, burn the inorganic carbon in high-temperature oxygen flow, convert the total organic carbon into carbon dioxide, and send the content of the total organic carbon through an infrared detector.\|[0004] However, the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, for example, for the coal-bearing formation, the rock sample may contain elemental carbon such as graphite and amorphous carbon, and the elemental carbon is stable at normal temperature and does not react with the dilute hydrochloric acid, so that the entire inorganic carbon in the rock sample cannot be removed by the dilute hydrochloric acid, which results in a higher content of the measured total organic carbon.\|DISCLOSURE\|Disclosure of Invention\|[0005] The invention aims to overcome the technical defects, and provides a method for measuring the total organic carbon content in rock, which solves the technical problem that the content of the measured total organic carbon is higher because simple substance carbon such as graphite, amorphous carbon and the like possibly contained in a rock sample is not removed in the method for measuring the total organic carbon content in the prior art.\|[0006] In order to achieve the technical purpose, the invention adopts the following technical scheme:\| the invention provides a method for measuring the content of total organic carbon in rock, which comprises the following steps: \| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope, and removing simple substance carbon in the crushed rock sample; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|[0007] In some embodiments, in step S1, the mass of the weighed rock fragments is 0.01-1.00g.\|[0008] In some embodiments, in step S2, the container is placed in a water bath, and the temperature of the water bath is controlled to be 60-80 ℃.\|[0009] In some embodiments, in step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by a sample washing device, where the sample washing device includes a cylinder and a screen, an opening at an upper end of the cylinder is provided, a water outlet is provided at a lower end of the cylinder, and the screen is detachably mounted at the opening at the upper end of the cylinder.\|[0010] In some embodiments, in step S4, the cleaned crushed rock is picked by a microscopic picking device, so as to remove elemental carbon in the crushed rock, where the microscopic picking device includes a base, a placing plate, a microscope, a position adjusting mechanism and a picking mechanism, the microscope is located above the base, the placing plate is used for placing the crushed rock on the base, the position adjusting mechanism is connected with the microscope and used for adjusting the position of an objective lens of the microscope, and the picking mechanism is used for sucking elemental carbon particles.\|[0011] In some embodiments, the position adjustment mechanism includes montant, vertical sliding sleeve, vertical screw, horizontal sliding sleeve, horizontal pole, horizontal screw and support, the lower extreme of montant is fixed in the base, vertical sliding sleeve locates the montant to extend along vertical direction, set up first screw on the vertical sliding sleeve, vertical screw threaded connection in first screw, and be used for with montant butt, horizontal sliding sleeve is fixed in vertical sliding sleeve to extend along the horizontal direction, the horizontal pole slides and inserts and locate in the horizontal sliding sleeve, the second screw has been seted up on the horizontal sliding sleeve, horizontal screw threaded connection in the second screw, and be used for with the horizontal pole butt, the support is fixed in the one end of horizontal pole, the support with microscope fixed connection.\|[0012] In some embodiments, the support is provided with an inclined hole arranged obliquely, the sampling mechanism comprises a transparent pipe, a blocking net, a suction pump and a connecting hose, the transparent pipe is slidably inserted into the inclined hole, the lower end of the transparent pipe is used for absorbing simple substance carbon on the object placing plate, the blocking net is fixed at the lower end of the transparent pipe, and an inlet of the suction pump is communicated with the upper end of the transparent pipe through the connecting hose.\|[0013] In some embodiments, in the step S4, the crushed rock sample after removing the elemental carbon is burned in a high-temperature oxygen stream by a total organic carbon content detection device, and the content of the generated carbon dioxide is detected by an infrared detector, so as to obtain the total organic carbon content of the rock sample, where the total organic carbon content detection device includes a burner, an oxygen inlet mechanism, a buffer mechanism and the infrared detector;\| The burner comprises a burner body, a combustion table and an igniter, wherein a closed combustion cavity is formed in the burner body, an air inlet communicated with the combustion cavity is formed in one end of the burner body, an air outlet communicated with the combustion cavity is formed in the other end of the burner body, the combustion table is arranged in the burner body, and the igniter is arranged in the burner body; \| the oxygen inlet mechanism comprises an oxygen tank, an outlet valve, an air pump and an output pipe, the outlet valve is arranged at the outlet of the oxygen tank, the inlet of the air pump is communicated with the outlet valve, the outlet of the air pump is communicated with one end of the output pipe, the other end of the output pipe is communicated with the air inlet, and the output pipe is provided with the output valve; \| The buffer mechanism comprises a buffer tank and a vacuum pump, wherein a gas inlet is formed in one end of the buffer tank, a gas outlet is formed in the other end of the buffer tank, the gas inlet is communicated with the gas outlet through a conduit, a gas guide valve is arranged on the conduit, the inlet of the vacuum pump is communicated with the gas outlet through a gas exhaust pipe, and the gas exhaust pipe is provided with a gas exhaust valve; \| The infrared detector is arranged in the cache tank. \|[0014] In some embodiments, a one-way valve is also provided on the output tube.\|[0015] In some embodiments, the buffer tank is provided with a pressure detecting member thereon.\|[0016] Compared with the prior art, the method for measuring the total organic carbon content in the rock has the beneficial effects that: removing inorganic carbon in a sample through dilute hydrochloric acid, picking under a microscope to remove simple substance carbon in the crushed rock sample, burning the crushed rock sample after removing the simple substance carbon in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and obtaining the content of the total organic carbon through an infrared detector.\|DRAWINGS DESCRIPTION\|[0017] Fig. 1 is a schematic structural diagram of a method for measuring total organic carbon content in rock according to an embodiment of the present invention.\|[0018] Fig. 2 is a schematic structural view of the sample washing apparatus used in step S3 in fig. 1.\|[0019] Fig. 3 is a schematic structural diagram of a microscopic picking device used in step S4 in fig. 1.\|[0020] Fig. 4 is a partial enlarged view of the area a in fig. 3.\|[0021] FIG. 5 is a schematic view of the microscope sampling device of FIG. 3 when the transparent tube is lifted.\|[0022] Fig. 6 is a schematic view of the microscope sampling device of fig. 5 at another perspective.\|[0023] Fig. 7 is a schematic structural diagram of the total organic carbon content detecting device used in step S5 in fig. 1.\|[0024] The reference numerals are 100-sample cleaning device, 110-cylinder, 111-water outlet, 120-screen, 200-microscopic sample picking device, 210-base, 220-object placing plate, 230-microscope, 240-position adjusting mechanism, 241-vertical rod, 242-vertical sliding sleeve, 243-vertical screw, 244-horizontal sliding sleeve, 245-horizontal rod, 246-horizontal screw, 247-bracket, 250-sample picking mechanism, 251-transparent tube, 252-blocking net, 300-total organic carbon content detecting device, 310-burner, 311-furnace body, 312-combustion table, 313-igniter, 320-oxygen inlet mechanism, 321-oxygen tank, 322-outlet valve, 323-air pump, 324-output pipe, 325-output valve, 326-one-way valve, 330-buffering mechanism, 331-buffering tank, 3311-pressure detecting piece, 332-vacuum pump, 333-conduit, 334-air guide valve, 335-air suction tube, 336-suction valve, 340-infrared detector.\|INVENTION MODE\|Detailed Description\|[0025] The present invention will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0026] In order to solve the technical problem that the content of the measured total organic carbon is higher because simple substance carbon such as graphite and amorphous carbon possibly contained in a rock sample is not removed in the total organic carbon content measuring method, the invention provides the total organic carbon content measuring method in the rock, and the accuracy of measuring the total organic carbon content can be improved.\|[0027] Referring to fig. 1, fig. 1 is a flow chart of a method for determining total organic carbon content in rock according to an embodiment of the invention, the method for determining total organic carbon content in rock includes the following steps:\| s1, grinding a rock sample, and weighing rock fragments with preset mass; \| S2, placing the weighed crushed rock sample into a container, adding excessive hydrochloric acid solution into the container, and reacting to remove inorganic carbon in the crushed rock sample; \| S3, washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water; \| S4, picking the cleaned crushed rock sample under a microscope to remove the simple substance carbon in the crushed rock sample, wherein the simple substance carbon in the rock is mainly graphite and amorphous carbon which are black, and the rock powder is usually light, so that the simple substance carbon can be easily identified and removed under the microscope; \| And S5, burning the crushed rock sample with the elemental carbon removed in a high-temperature oxygen stream, and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample. \|[0028] According to the technical scheme provided by the invention, after inorganic carbon in a sample is removed through dilute hydrochloric acid, sample picking is performed under a microscope to remove simple substance carbon in the rock fragments, then the rock fragments after simple substance carbon removal are combusted in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and the content of the total organic carbon is obtained through an infrared detector.\|[0029] In one embodiment, referring to fig. 1, in the step S1, the rock sample is ground to a particle size of less than 0.2mm, the mass of the ground sample is not less than 10g, and in the step S1, the mass of the weighed crushed rock sample is 0.01-1.00g, and is accurate to 0.0001g.\|[0030] In one embodiment, referring to fig.1, in the step S2, the container is placed in a water bath, the temperature of the water bath is controlled to be 60-80 ℃, and the sample is dissolved for more than 2 hours until the reaction is complete.\|[0031] In one embodiment, referring to fig. 1 and 2, in step S3, the crushed rock sample after hydrochloric acid treatment is washed to be neutral by the sample washing device 100, the sample washing device 100 includes a cylinder 110 and a screen 120, an upper end opening of the cylinder 110 is disposed, a water outlet 111 is disposed at a lower end of the cylinder 110, and the screen 120 is detachably mounted at the upper end opening of the cylinder 110. In use, the crushed rock sample after hydrochloric acid treatment is poured into the screen 120, and distilled water boiled is continuously introduced into the screen until the pH value of the crushed rock sample is neutral.\|[0032] In one embodiment, referring to fig. 1 and 3, in step S4, the cleaned crushed rock is picked by a microscopic picking device 200 to remove elemental carbon in the crushed rock, the microscopic picking device 200 includes a base 210, a placing plate 220, a microscope 230, a position adjusting mechanism 240, and a picking mechanism 250, the microscope 230 is located above the base 210, the placing plate 220 is used for placing the crushed rock on the base 210, the position adjusting mechanism 240 is connected with the microscope 230 and is used for adjusting the position of an objective lens of the microscope 230, and the picking mechanism 250 is used for sucking elemental carbon particles.\|[0033] In one embodiment, please refer to fig. 3-6, the position adjusting mechanism 240 includes a vertical rod 241, a vertical sliding sleeve 242, a vertical screw 243, a horizontal sliding sleeve 244, a cross rod 245, a horizontal screw 246 and a support 247, wherein the lower end of the vertical rod 241 is fixed in the base 210, the vertical sliding sleeve 242 is slidably sleeved on the vertical rod 241 and extends along the vertical direction, a first screw hole is formed in the vertical sliding sleeve 242, the vertical screw 243 is in threaded connection with the first screw hole and is used for being in butt joint with the vertical rod 241, the horizontal sliding sleeve 244 is fixed in the vertical sliding sleeve 242 and extends along the horizontal direction, the cross rod 245 is slidably inserted in the horizontal sliding sleeve 244, a second screw hole is formed in the horizontal sliding sleeve 244, the horizontal screw 246 is in threaded connection with the second screw hole and is used for being in butt joint with the cross rod 245, the support 247 is fixed at one end of the cross rod 245, the support 247 is fixedly connected with the microscope 230, and when in use, the vertical screw 243 is unscrewed, namely, the vertical sliding sleeve 242 is in threaded connection with the first screw hole, and is used for being in threaded connection with the vertical sliding sleeve 241, so as to enable the vertical sliding sleeve 241 to rotate around the microscope 241, thereby enable the vertical sliding sleeve 241 to rotate around the vertical rod 241, and the microscope 241 to reach the position of the microscope 230, and the position of the microscope 230 can be changed, and the position of the microscopic plate 220 can be different from the position of the microscopic plate 220, and the microscopic plate 220 can be in turn, or the position of the microscopic plate 220, and the position can be changed.\|[0034] In one embodiment, referring to fig. 3-6, the support 247 is provided with an inclined hole, the sample picking mechanism 250 includes a transparent tube 251, a blocking net 252, a suction pump (not shown) and a connection hose (not shown), the transparent tube 251 is slidably inserted into the inclined hole, the lower end of the transparent tube 251 is used for sucking the elemental carbon on the object placing plate 220, the blocking net 252 is fixed at the lower end of the transparent tube 251, the inlet of the suction pump is communicated with the upper end of the transparent tube 251 through the connection hose, when in use, the lower end of the transparent tube 251 is aligned with the elemental carbon, then the suction pump is started, the elemental carbon is sucked into the transparent tube 251 by the blocking net 252, then the transparent tube 251 is lifted, then the material receiving box is placed at the lower end of the transparent tube 251, then the suction pump is closed, and the elemental carbon in the transparent tube 251 falls into the material receiving box under the action of gravity, thereby removing the elemental carbon.\|[0035] In one embodiment, referring to fig. 1 and 7, in step S4, a crushed rock sample from which elemental carbon is removed is burned in a high-temperature oxygen stream by a total organic carbon content detection device 300, and the content of carbon dioxide generated is detected by an infrared detector to obtain the total organic carbon content of the rock sample, where the total organic carbon content detection device 300 includes a burner 310, an oxygen inlet mechanism 320, a buffer mechanism 330, and an infrared detector 340;\| the burner 310 comprises a burner body 311, a burner table 312 and an igniter 313, wherein a sealed combustion cavity is arranged in the burner body 311, an air inlet communicated with the combustion cavity is formed in one end of the burner body 311, an air outlet communicated with the combustion cavity is formed in the other end of the burner body 311, the burner table 312 is arranged in the burner body 311, and the igniter 313 is arranged in the burner body 311; \| The oxygen inlet mechanism 320 comprises an oxygen tank 321, an outlet valve 322, an air pump 323 and an output pipe 324, the outlet valve 322 is arranged at the outlet of the oxygen tank 321, the inlet of the air pump 323 is communicated with the outlet valve 322, the outlet of the air pump 323 is communicated with one end of the output pipe 324, the other end of the output pipe 324 is communicated with the air inlet, and the output pipe 324 is provided with an output valve 325; \| The buffer mechanism 330 comprises a buffer tank 331 and a vacuum pump 332, wherein a gas inlet is formed at one end of the buffer tank 331, a gas outlet is formed at the other end of the buffer tank 331, the gas inlet is communicated with the gas outlet through a conduit 333, a gas guide valve 334 is arranged on the conduit 333, an inlet of the vacuum pump 332 is communicated with the gas outlet through a gas exhaust pipe 335, and a gas exhaust valve 336 is arranged on the gas exhaust pipe 335; \| the infrared detector 340 is disposed in the buffer tank 331. \|[0036] The detection flow of the total organic carbon content detection device 300 is as follows:\| (1) Uniformly mixing the crushed rock sample after removing the simple substance carbon with the scrap iron cosolvent and the tungsten particle cosolvent, and placing the mixture in a combustion table 312; \| (2) Vacuumizing, closing the outlet valve 322, opening the output valve 325, the air guide valve 334 and the air extraction valve 336, and then opening the vacuum pump 332, wherein the vacuum pump vacuumizes the buffer tank 331, the oxygen tank 321 and the pipeline; \| (3) Oxygen is introduced, the air extraction valve 336 and the air guide valve 334 are closed, the outlet valve 322 is opened, and sufficient oxygen is introduced into the combustion chamber; \| (4) The igniter 313 ignites the sample on the combustion table 312, continuously introduces oxygen, and then opens the outlet valve 322 to introduce the generated gas into the buffer tank 331; \| (5) After full combustion, the output valve 325 is closed, combustion is stopped, after the system is stable, the carbon dioxide concentration in the buffer tank 331 is detected through the infrared detector 340, the carbon dioxide concentration in the buffer tank 331 is equal to the carbon dioxide concentration in the furnace body 311, the total amount of carbon dioxide generated by combustion can be obtained according to the carbon dioxide concentration multiplied by the total volume of the buffer tank 331, the furnace body 311 and the auxiliary pipeline, the total amount of organic carbon in the crushed rock sample is further obtained, and the total organic carbon content in the crushed rock sample can be obtained by dividing the total amount by the mass of the crushed rock sample. \|[0037] In one embodiment, referring to fig. 1 and 7, the output pipe 324 is further provided with a check valve 326, so as to avoid reverse flow of the gas.\|[0038] In one embodiment, referring to fig. 1 and 7, a pressure detecting member 3311 is provided on the buffer tank 331 to facilitate control of the reaction pressure.\|[0039] According to the technical scheme provided by the invention, after inorganic carbon in a sample is removed through dilute hydrochloric acid, sample picking is performed under a microscope to remove simple substance carbon in the rock fragments, then the rock fragments after simple substance carbon removal are combusted in high-temperature oxygen flow to convert total organic carbon into carbon dioxide, and the content of the total organic carbon is obtained through an infrared detector.\|[0040] The above-described embodiments of the present invention do not limit the scope of the present invention. Any other corresponding changes and modifications made in accordance with the technical idea of the present invention shall be included in the scope of the claims of the present invention.	Family Number\|(113895166)\|113895166\|Object of Invention\|(CN119666501 A)\|( . . . ) solution into the container , washing the rock fragments subjected to hydrochloric acid treatment to be neutral through distilled water , picking the washed rock fragments under a microscope , burning the rock fragments subjected to simple substance carbon removal in high - temperature oxygen flow , and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample . \|Abstract\|(CN119666501 A)\|The invention discloses a method for determining the total organic carbon content in rock , which comprises the following steps : grinding a rock sample , and weighing a preset mass of crushed rock sample ; putting the weighed crushed rock sample into a container , and adding an excessive hydrochloric acid solution into the container ; washing the crushed rock sample treated by hydrochloric acid with distilled water until the crushed rock sample is neutral ; picking the cleaned broken rock sample under a microscope ; burning the broken rock sample with the elemental carbon removed in high - temperature oxygen flow , and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample . The method has the beneficial effects that after inorganic carbon in the sample is removed through diluted hydrochloric acid , the sample is picked under a microscope , simple substance carbon in the crushed rock sample is removed , then the crushed rock sample with the simple substance carbon removed is combusted in high - temperature oxygen flow , the total organic carbon is converted into carbon dioxide , the content of the total organic carbon is obtained through an infrared detector , and the content of the total organic carbon in the crushed rock sample is calculated . And the accuracy of the total organic carbon content determination result can be improved . \|Independent Claims\|(CN119666501 A)\|( . . . ) S2 , placing the weighed crushed rock sample into a container , adding excessive hydrochloric acid solution into the container , and reacting to remove inorganic carbon in the crushed rock sample ; S3 , washing the crushed rock sample subjected to hydrochloric acid treatment to be neutral through distilled water ; S4 , picking the cleaned crushed rock sample under a microscope , and removing simple substance carbon in the crushed rock sample ; And S5 , burning the crushed rock sample with the elemental carbon removed in a high - temperature oxygen stream , and detecting the content of the generated carbon dioxide by an infrared detector to obtain the total organic carbon content of the rock sample . \|	Measurement				G01N-001/28\|G01N-021/3504\|G01N-031/12	G01N-001/28\|G01N-021/3504\|G01N-031/12					CN118455193\|CN221516634U\|CN116884909\|CN219161963U\|CN215833688U\|CN113533619\|CN113030192\|CN110987767\|CN110044677\|CN107132098\|CN106442096\|CN104931310\|DE102012007348\|US20090078885	CN118455193 110987371 WHO=Examiner SELF=N CAT=A\|CN221516634U 111021276 WHO=Examiner SELF=N CAT=A\|CN116884909 106849386 WHO=Examiner SELF=N CAT=A\|CN219161963U 105258783 WHO=Examiner SELF=N CAT=A\|CN215833688U 98704829 WHO=Examiner SELF=N CAT=A\|CN113533619 96639665 WHO=Examiner SELF=N CAT=A\|CN113030192 94887941 WHO=Examiner SELF=N CAT=A\|CN110987767 88258761 WHO=Examiner SELF=N CAT=A\|CN110044677 85425821 WHO=Examiner SELF=N CAT=A\|CN107132098 77170469 WHO=Examiner SELF=N CAT=A\|CN106442096 75490447 WHO=Examiner SELF=N CAT=A\|CN104931310 70927439 WHO=Examiner SELF=N CAT=A\|DE102012007348 46165021 WHO=Examiner SELF=N CAT=A\|US20090078885 14120924 WHO=Examiner SELF=N CAT=A	浮爱青等: "沉积岩中总有机碳测定的方法验证", 《广州化学》, vol. 43, no. 05, 31 October 2018 (2018-10-31), pages 39 - 43 (Cat. Y,X)\|欧阳泉根等: "盐酸预处理-高频燃烧红外吸收法测定含铀岩石中有机碳", 《冶金分析》, vol. 40, no. 02, 29 February 2020 (2020-02-29), pages 18 - 23 (Cat. A)	CN104931310; CN106442096; CN107132098; CN110044677; CN113030192; CN113533619; CN215833688U; CN219161963U; CN116884909; CN221516634U; US20090078885; DE102012007348; CN110987767; CN118455193		PENDING	(CN119666501)\|PENDING	ALIVE	(CN119666501)\|ALIVE	(CN119666501)\|LEGAL DETAILS FOR CN119666501\|Actual or expected expiration date=2044-12-05\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-12-05\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202411779739\|Application date=2024-12-05\|Standardized application number=2024CN-1779739\|Event publication date=2025-03-21\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN119666501\|Publication stage code=A\|Publication date=2025-03-21\|Standardized publication number=CN119666501\|Event publication date=2025-03-21\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2025-04-08\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN119666501)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQRk0YvrOuH8Ffn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000076894002&ekey=2029&xpn=CN119666501&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=4oF3kmNZA1WO6CzMQqwYZpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN119666501)\|CN	(CN119666501)\|NAME=SHAANXI YANCHANG PETROLEUM (GROUP) CO. LTD. , COUNTRY=CN		(CN119666501)\|NAME=HE SHAN;XIAN YINUO PATENT AGENT CO. LTD. , REG=61220		(CN119666501)\|NAME=LIU SHUANGSHUANG\|NAME=CUI PENGXING\|NAME=LIU LILI\|NAME=KANG SHENGSONG\|NAME=ZHAO XUESI\|NAME=WANG TAO\|NAME=ZHU TONGTONG	(CN119666501)\|7	1	1					(CN119666501)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2025-03-21\|Gazette number: GAZNUM=41-1202\|Number of Pages: NPAGES=12\|		(CN119666501)\|CHINESE (CHI)	(CN119666501)\|Patent	Titre: (CN119666501)\|Method for determining total organic carbon content in rock Résumé: (CN119666501)\|The invention discloses a method for determining the total organic carbon content in rock, which comprises the following steps: grinding a rock sample, and weighing a preset mass of crushed rock sample; putting the weighed crushed rock sample into a container, and adding an excessive hydrochloric acid solution into the container; washing the crushed rock sample treated by hydrochloric acid with distilled water until the crushed rock sample is neutral; picking the cleaned broken rock sample under a microscope; burning the broken rock sample with the elemental carbon removed in high-temperature oxygen flow, and detecting the content of generated carbon dioxide through an infrared detector to obtain the total organic carbon content of the rock sample. The method has the beneficial effects that after inorganic carbon in the sample is removed through diluted hydrochloric acid, the sample is picked under a microscope, simple substance carbon in the crushed rock sample is removed, then the crushed rock sample with the simple substance carbon removed is combusted in high-temperature oxygen flow, the total organic carbon is converted into carbon dioxide, the content of the total organic carbon is obtained through an infrared detector, and the content of the total organic carbon in the crushed rock sample is calculated. And the accuracy of the total organic carbon content determination result can be improved.	12	Abstract	gpt-4o-mini	no	The article focuses on a method for determining total organic carbon content in rock, which does not relate to accelerated weathering or CO₂ capture.
15	GB202319995	WOGB2024/051780\|GB202319995	GB2636853\|WO2025/133560\|GB202319995	108540136	WO2025/133560 A1 2025-06-26 [WO2025133560]\|GB2636853 A 2025-07-02 [GB2636853]\|GB202319995 D0 2024-02-07 [GB202319995]	2023-12-22	2024-07-08\|2023-12-22	2025-07-02\|2025-06-26\|2024-02-07		(WO2025/133560)\|2027-06-22\|(GB2636853)\|2043-12-22	(WO2025/133560)\|Enhanced weathering carbon dioxide removal quantification method and apparatus	(WO2025/133560)\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water. Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal.	UNDO CARBON	(WO2025/133560)\|UNDO CARBON LTD ([GB])\|(GB2636853)\|Undo Carbon Ltd\|(GB202319995)\|Undo Carbon Ltd	LIU XINRAN	(WO2025/133560)\|LIU, Xinran	(WO2025/133560)\|BARNES IP LIMITED ([GB])	(WO2025/133560)\|However, when the soil has a low moisture content, it is difficult to extract enough moisture from the soil to get reliable data.\|Should the soil contain too little moisture, for example in circumstances where there has been little rainfall (e.g. when there has been a droughtfor a number of months), it becomes difficult to extract enough water from a soil sample to conduct normal tests of the pore water.\|	(WO2025/133560)\|1. A method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removing the soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850).\|	(WO2025/133560)\|According to a first aspect, there is provided method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removing the soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850).\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore soil water.\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water.\|	(WO2025/133560)\|SOIL SAMPLE(100,77)\|CARBON DIOXIDE(100,18)\|ENHANCED WEATHERING(100,11)\|PORE WATER SAMPLE(100,5)\|ENHANCED WEATHERING CARBON DIOXIDE(100,2)\|REMOVAL QUANTIFICATION(100,2)\|ENHANCED WEATHERING PRODUCT(67,2)\|ACIDIFIED DRIED SOIL SAMPLE(64,6)\|GROUND(61,39)\|MOISTURE CONTENT(55,6)\|CARBON DIOXIDE REMOVAL(50,4)\|ENOUGH MOISTURE(50,1)\|DROUGHT(46,1)\|CENTRIFUGE SPENT CORE SOLUTION(45,2)\|RAINFALL(44,2)\|PORE WATER EXTRACTION(40,2)\|PORE SOIL WATER(38,1)\|TREATED DRIED SOIL SAMPLE(36,4)\|RELIABLE DATA(36,1)\|STERILIZED DISTILLED WATER BATH(33,3)\|FACTOR CHANGE(30,2)\|DRAINAGE(28,2)\|AMMONIUM ACETATE SOLUTION(26,6)\|MONTH NUMBER(26,1)\|ENHANCED WEATHERING OPERATION(25,5)\|ARTIFICIAL RAIN WATER(24,3)\|GRAVEL(19,11)\|WATER CONTENT(18,5)\|OVEN(18,3)\|PORE WATER(17,10)\|ULTRAHIGH PURITY WATER(17,3)\|CRUSHED ROCK GEOCHEMICAL(16,1)\|SOIL CORE SAMPLE CONTAINER(14,6)\|MOISTURE PROBE(14,2)\|NITRIC ACID(14,2)\|MACRO RHYZON(14,1)\|EXTRACTING WATER CONTENT(12,3)\|ENHANCING SOIL(11,2)\|FARM MACHINERY(10,3)\|ANALYTICAL GRADE AMMONIUM ACETATE(10,1)\|ANALYTICAL GRADE AMMONIUM HYDROXIDE(10,1)\|MEASUREMENT OPTION(10,1)\|ROCK PARTICLE(10,1)\|TOTAL CATION QUANTIFICATION(10,1)\|TREATED SPENT CORE(10,1)\|RPM(9,4)\|SEA(9,3)\|BICARBONATE(8,2)\|CARBON DIOXIDE CAPTURE(8,2)\|TRAILER(8,2)\|ANALYTICAL GRADE ACETIC ACID(8,1)\|CATION CONTENT(8,1)\|CENTRIFUGE EQUIPMENT(8,1)\|DISPERSION(8,1)\|ENHANCED WEATHERING OPERATOR(8,1)\|MODELED CARBON CAPTURE(8,1)\|PARAMETER CALCULATION(8,1)\|SAMPLE DRY LAND(8,1)\|SPREADING CRUSHED SILICATE(8,1)\|STANDARD CENTRIFUGE(8,1)\|ULTRA HIGH PURITY WATER(8,1)\|BOTTOM LID(6,3)\|ADDING CRUSHED ROCK(6,1)\|ALKALINITY(6,1)\|BASALT(6,1)\|CENTRIFUGATION(6,1)\|ENHANCED WEATHERING PERFORMANCE(6,1)\|ENHANCED WEATHERING REACTION(6,1)\|FASTENING(6,1)\|LABORATORY(6,1)\|\|(GB2636853)\|SOIL SAMPLE(100,58)\|CARBON DIOXIDE(100,15)\|ENHANCED WEATHERING(100,9)\|PORE WATER SAMPLE(100,4)\|ENHANCED WEATHERING CARBON DIOXIDE(100,1)\|REMOVAL QUANTIFICATION(100,1)\|ENOUGH MOISTURE(38,1)\|GROUND(36,31)\|DROUGHT(35,1)\|RAINFALL(33,2)\|ENHANCED WEATHERING PRODUCT(32,1)\|MOISTURE CONTENT(30,5)\|PORE SOIL WATER(29,1)\|RELIABLE DATA(27,1)\|STERILIZED DISTILLED WATER BATH(25,3)\|DRAINAGE(21,2)\|MONTH NUMBER(20,1)\|CARBON DIOXIDE REMOVAL(19,2)\|ARTIFICIAL RAIN WATER(18,3)\|GRAVEL(14,11)\|WATER CONTENT(13,5)\|CRUSHED ROCK GEOCHEMICAL(12,1)\|ENHANCED WEATHERING OPERATION(10,4)\|MOISTURE PROBE(10,2)\|MACRO RHYZON(10,1)\|PORE WATER(9,9)\|EXTRACTING WATER CONTENT(9,3)\|FARM MACHINERY(7,3)\|SEA(7,3)\|MEASUREMENT OPTION(7,1)\|ROCK PARTICLE(7,1)\|BICARBONATE(6,2)\|CARBON DIOXIDE CAPTURE(6,2)\|TRAILER(6,2)\|1M HCL(6,1)\|CATION CONTENT(6,1)\|CENTRIFUGE EQUIPMENT(6,1)\|DISPERSION(6,1)\|ENHANCED WEATHERING OPERATOR(6,1)\|ENHANCING SOIL(6,1)\|MODELED CARBON CAPTURE(6,1)\|PARAMETER CALCULATION(6,1)\|SAMPLE DRY LAND(6,1)\|SPREADING CRUSHED SILICATE(6,1)\|STANDARD CENTRIFUGE(6,1)\|BOTTOM LID(5,3)\|ADDING CRUSHED ROCK(4,1)\|ALKALINITY(4,1)\|BASALT(4,1)\|ENHANCED WEATHERING PERFORMANCE(4,1)\|ENHANCED WEATHERING REACTION(4,1)\|FASTENING(4,1)\|LABORATORY(4,1)\|NEIGHBORING WATER MOLECULE(4,1)\|OUTGASSING(4,1)\|QUANTIFICATION(4,1)\|	(WO2025/133560)\|CLAIMS: \|1. A method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removing the soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850).\|2. The method of any preceding claim, wherein the soil sample is contained in a sample tube.\|3. The method of claim 2 wherein the sample tube is substantially made from metal and/or is substantially cylindrical.\|4. The method of either claims 2 or 3 wherein the sample tube comprises one or more caps, the one or more caps operable to seal the contents of the sample tube.\|5. The method of any preceding claim, wherein the bath of water comprises a bath of sterilised distilled water.\|6. The method of any preceding claim, wherein the step of placing the soil sample in a bath of water comprising placing the soil sample in the bath of water for substantially 24 hours and/or at substantially 2 to 4 degrees Celsius.\|7. The method of any preceding claim, wherein the step of removing the soil sample from the bath of water comprising removing the soil sample from the bath of water for sufficient duration to allow free drainage.\|8. The method of any preceding claim, wherein the step of applying pressure to the soil sample comprises placing the soil sample in a centrifuge.\|9. The method of claim 8 wherein the centrifuge spins the soil sample for substantially 30 minutes and/or at substantially 1 ,000 revolutions per minute.\|10. The method of any preceding claim further comprising the step of filtering the extracted water content.\|11. The method of claim 10 wherein the step of filtering is performed for substantially 5 to 10 minutes.\|12. The method of any preceding claim further comprising: drying the soil sample to create a dried soil sample; combining the dried soil sample with an ammonium acetate solution to create a spent core solution; applying pressure to the spent core solution; filtering the spent core solution to remove a treated dried soil sample; further treating the treated dried soil sample with an acid to create an acidified dried soil sample; and analysing the acidified dried soil sample to determine a measurement of cations in the acidified dried soil sample.\|13. The method of claim 12 wherein drying the soil sample comprising drying the soil sample in an oven and optionally crushing and/or mixing and/or sieving the soil sample to create the dried soil sample.\|14. The method of claims 12 or 13 further comprising the step of placing the dried soil sample in a rotating shaking apparatus.\|15. The method of any of claims 12 to 14, wherein applying pressure to the spent core solution comprises using a centrifuge apparatus to centrifuge the spent core solution.\|16. The method of any of claims 12 to 15 wherein the acid is nitric acid.\|17. The method of any of claims 12 to 16 wherein the ammonium acetate solution comprises any combination of: ammonium acetate; ammonium hydroxide; and ultra- high purity water.	(WO2025/133560)\|[0001] ENHANCED WEATHERING CARBON DIOXIDE REMOVAL QUANTIFICATION METHOD AND APPARATUS \| [0002] Field \| [0003] The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore soil water. \| [0004] Background \| [0005] Enhanced weathering is the process of spreading suitable crushed silicate rock materials over suitable land, such as farmland. Suitable rock materials include rock such as basalt, which naturally reacts with dissolved carbon dioxide in the form of carbonic acid to remove the carbon dioxide from the environment. By crushing the rock, the crushed rock has a larger surface area per particle which speeds up the process of capturing carbon dioxide by increasing the reaction surface area. By spreading the rock over, for example, farmland, carbon dioxide can be captured over a large land surface. \| [0006] During enhanced weathering, it is important to measure the properties of the enhanced weathering reaction in order to measure the amount of carbon dioxide captured in the soil, rivers and eventually oceans. This data can be used to compare against modelled carbon capture, verify carbon credits, or plan further enhanced weathering based on weathering performance. \| [0007] To measure enhanced weathering, one of the measurement options is to extract pore water using a tool called a macro rhyzon in order to determine the level of carbon capture from the sample or samples is obtained. However, when the soil has a low moisture content, it is difficult to extract enough moisture from the soil to get reliable data. \| [0008] Summary of Invention \| [0009] Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. \| [0010] According to a first aspect, there is provided method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removingthe soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850). \| [0011] By allowing the soil sample to be placed in water, the soil sample can saturate with water and this can allow the subsequent removal of both the added water and the original water content for subsequent testing. This can allow the testing of water in a soil sample containing substantially too low a moisture content to provide sufficient water for normal pore water testing. \| [0012] Optionally, the soil sample is contained in a sample tube. Optionally, the sample tube is substantially made from metal and/or is substantially cylindrical. Optionally, the sample tube comprises one or more caps, the one or more caps operable to seal the contents of the sample tube. \| [0013] The soil sample can be contained in a variety of configurations of sample apparatus, but can typically be obtained using a configuration of sample apparatus that is operable to work with a standard centrifuge and/or standard configuration of mechanical pressure apparatus. \| [0014] Optionally, the bath of water comprises a bath of sterilised distilled water. \| [0015] In other embodiments, artificial rainwater can be used. Using sterilised distilled water and/or artificial rainwater can allow the extracted water content to retain substantially all of the properties desired to be measured. \| [0016] Optionally, the step of placing the soil sample in a bath of water comprising placing the soil sample in the bath of water for substantially 24 hours and/or at substantially 2 to 4 degrees Celsius. \| [0017] Placing the soil sample in a bath of water under substantially these conditions can allow the soil sample to saturate with the water contained in the bath and/or substantially not change the properties of the soil sample and/or its water content. \| [0018] Optionally, the step of removing the soil sample from the bath of water comprising removing the soil sample from the bath of water for sufficient duration to allow free drainage. \| [0019] Removing the soil sample from the bath of water can allow only water that has been absorbed by the soil sample to remain prior to further step of the process being performed. \| [0020] Optionally, the step of applying pressure to the soil sample comprises placing the soil sample in a centrifuge. \| [0021] Placing the soil sample in a centrifuge can remove the moisture content of the soil substantially quickly, and/or causes water molecules being removed from the soil sample during the centrifuge operation to pull neighbouring water molecules out of the soil sample. \| [0022] Optionally, the centrifuge spins the soil sample for substantially 30 minutes and/or at substantially 1 ,000 revolutions per minute.Using this configuration of centrifuge equipment can allow sufficient water to be removed from the soil sample to allow subsequent tests to be performed on a substantially sufficient sample size. \| [0023] Optionally, the method further comprises the step of filtering the extracted water content. Optionally, the step of filtering is performed for substantially 5 to 10 minutes. \| [0024] By filtering the water, debris such as soil can be removed which might otherwise impact the measurements/analysis performed on the extracted water. \| [0025] Optionally, the method further comprises drying the soil sample to create a dried soil sample; combining the dried soil sample with an ammonium acetate solution to create a spent core solution; applying pressure to the spent core solution; filtering the spent core solution to remove a treated dried soil sample; further treating the treated dried soil sample with an acid to create an acidified dried soil sample; and analysing the acidified dried soil sample to determine a measurement of cations in the acidified dried soil sample. Optionally drying the soil sample comprising drying the soil sample in an oven and optionally crushing and/or mixing and/or sieving the soil sample to create the dried soil sample. Optionally, the method further comprises the step of placing the dried soil sample in a rotating shaking apparatus. Optionally applying pressure to the spent core solution comprises using a centrifuge apparatus to centrifuge the spent core solution. Optionally the acid is nitric acid. Optionally, the ammonium acetate solution comprises any combination of: ammonium acetate; ammonium hydroxide; and ultra-high purity water. \| [0026] By treating the “spent core” samples using ammonium acetate solution and analysing the treated spent cores, it is possible to measure the cations in the spent core and therefore at the site from which the core was obtained. \| [0027] Brief Description of Drawings \| [0028] Embodiments will now be described, by way of example only and with reference to the accompanying drawings having like-reference numerals, in which: \| [0029] Figure 1 shows an example enhanced weathering process; \| [0030] Figure 2 shows an example of a soil core sample container; \| [0031] Figure 3 shows an example of the use of the soil core sample container, prior to insertion into the soil to be sampled; \| [0032] Figure 4 shows an example of the use of the soil core sample container to insert into the soil to be sampled; \| [0033] Figure 5 shows an example of the use of the soil core sample container being removed from the soil to be sampled;Figure 6 shows an example of the use of the soil core sample container to contain the soil to be sampled; \| [0034] Figure 7 shows an example of the use of the soil core sample container being secured for transport with the soil sample inside; and \| [0035] Figure 8 shows an embodiment of the enhanced soil core moisture process. \| [0036] Specific Description \| [0037] Referring to Figure 1 , an example of an enhanced weathering process 100 will now be described. \| [0038] Enhanced weathering is performed by adding crushed rock 130 to farmland 140. In this described embodiment, the crushed rock 130 is added using farm machinery 120 such as a tractor with a trailer containing the crushed rock 130, where the trailer is configured to disperse the crushed rock 130 in a predetermined dispersal rate over substantially all of the surface of the farmland 140 as the farm machinery 120 travels along the farmland 140, typically travelling along parallel lines back and forth along the farmland 140. \| [0039] Not all of the land needs to be subject to enhanced weathering, so in this embodiment farmland 140 undergoes the enhanced weathering process 100 but non-weathered land 110 does not have any crushed rock 130 spread over its surface. \| [0040] In this embodiment, the properties of the farmland 140 that is to be subject to the enhanced weathering process 100 are determined in advance based on a combination of data for the area in which the farmland 140 is located along with data collected from the farmland 140. This data includes expected rainfall, pH, soil composition. Other data that is used as part of the process 100 is data pertaining to the crushed rock 130, including geochemical properties of the crushed rock and the range of surface area of the rock particles. Using this data, the amount of crushed rock 130 to spread over the farmland 140 and the density of spread/amount to be spread over the farmland 140 is calculated in advance of the spreading operation by the farm machinery 120. \| [0041] In other embodiments, different data can be obtained in advance of the spreading operation. In other embodiments, a spreading plan can comprise different arrangements for different parts of the farmland 140, for example differing amounts of rock to be spread on different portions of the farmland 140. In other embodiments, different equipment can be used to spread the crushed rock 130. In other embodiments, multiple spreading operations may be performed at one or more time intervals. In other embodiments, sensors can be used to monitor the properties of the farmland 140, before and/or after the one or more spreading operations being performed.Following the enhanced weathering operation 100, carbon dioxide is absorbed from the atmosphere above the farmland 140 by a chemical reaction between the dissolved carbon dioxide and the crushed rock 130 spread over the surface of the farmland 140. This captures and sequesters carbon dioxide from the atmosphere into the soil over substantially the entire area that has been subject to enhanced weathering operations 100. Depending on the parameters that have been calculated for the rock spreading operation(s), the rate of carbon dioxide capture depends on the amount and properties of the crushed rock 130 that has been spread over the farmland 140 and a prediction for this carbon dioxide capture will be determined from the calculated parameters for the rock spreading operation(s). \| [0042] Following the enhanced weathering operation 100, one of the measurements that needs to be performed to verify the amount of carbon captured is to measure the properties of the water in the soil, specifically the pore water. Pore water measurements can be key to understanding the soil chemistry and therefore how much carbon dioxide has been removed from the atmosphere. Enhanced weathering performance can depend on the pore water leaving the soil via the normal channels (e.g. streams and rivers) and reaching the ocean. Therefore, operators of enhanced weathering processes typically measure the contents of water in fields undergoing enhanced weathering to demonstrate bicarbonate and cation content in the pore water, which then leaves the soil and in time enters the ocean. \| [0043] Should the soil contain too little moisture, for example in circumstances where there has been little rainfall (e.g. when there has been a droughtfor a number of months), it becomes difficult to extract enough water from a soil sample to conduct normal tests of the pore water. If this is the case then the following process can be used to obtain sufficient water from soil that contains too little moisture. \| [0044] Pore water samples also should be analysed within around 36 hours of taking the sample, as the partial pressure of carbon dioxide in soil is different to that in air, so over time there is outgassing and degradation of the data (e.g. the bicarbonates in the soil sample will typically degrade over time as the pressure equilibrium moves from that of soil to that of air) that can be obtained from the pore water if tests aren’t performed promptly. \| [0045] Simply applying a large degree of pressure to the soil samples may not be possible is the moisture content is too low, as there is a limit to the amount of mechanical suction/pressure that is possible and depending on the type of soil it becomes impossible to extract sufficient water once the moisture levels drop below a certain level (this level varies by soil composition). Some methods of suction/pressure can extract sufficient water from soil samples but take too long, and after 36 hours from taking the soil sample the water extracted doesn’t provide a representative sample for analysis. \| [0046] Referring to Figure 2, an example soil core sample container 200 will now be described.The sample tube 220 is a hollow metal cylinder, which has two caps or lids, a top lid 210 and a bottom lid 230. The top and bottom lids 210, 230 are designed to fit on to the open ends of the tube 220 to secure and seal the sample soil contained within the sample tube 220. In this embodiment the caps 210, 230 fit to the ends of the tube 220 by an interference fit. In other embodiments, the caps 210, 230 can use a screw thread to fit to the tube 220. In other embodiments, other fixing mechanisms can be used to secure the lids 210, 230 to the tube 220. In this embodiment, each cylinder has a 5cm diameter and is 5cm deep. \| [0047] Typically, in this embodiment, multiple samples will be taken each with separate soil core sample containers, commensurate to the area of land being sampled. \| [0048] Referring to Figure 3, an example of use 300 of the soil core container of Figure 2 will now be described. \| [0049] A sample tube 310 (as described above in relation to Figure 2) is shown in this embodiment without caps. It is positioned above the surface of the soil 320. The intention is to sample a core of soil by inserting the sample tube 310 into the soil surface 320 to obtain a core of soil within the sample tube 310. \| [0050] Referring to Figure 4, an example of soil sampling 400 using the soil core container of Figure 2 will now be described. \| [0051] The sample tube 410 is inserted 440 into the soil, penetrating the soil surface 420 and thereby causing a sample of soil 430 to enter into the sample tube 410. In this embodiment, the tube 410 is hammered into the soil. \| [0052] Referring to Figure 5, an example of soil sample removal 500 using the soil core container of Figure 2 will now be described. \| [0053] The sample tube 510 is removed 540 from the soil surface 520, leaving a hole 550 and with the soil sample 530 contained within the sample tube 510. The soil sample 530 typically stays within the sample tube 510 when it is removed from the ground. It is typically very important to keep the soil core as a solid undisturbed soil sample hence it is kept intact within the cylinder 510. \| [0054] Referring to Figure 6, an example of securing the soil 600 within the soil core container of Figure 2 will now be described. \| [0055] The sample tube 610 containing the soil sample 630 then has the two lids 620, 640 placed at either open end of the cylinder 610 containing the soil sample 630. \| [0056] The top lid 620 is fit over one end of the sample tube 610 using an interference fit. The bottom lid 640 is fit over the other end of the sample tube 610 using an interference fit. The lids 620, 640 prevent the soil or any moisture from leaving the interior of the sample tube 610. \| [0057] In other embodiments, other fastening mechanisms can be used to fasten the lids 620, 640 to the tube 610.Referring to Figure 7, an example of readying the soil sample for transport 700 using the soil core container of Figure 2 will now be described. \| [0058] The sample tube 710 is shown with both lids 720, 740 securely fastened over either open end of the cylinder 710 containing the soil sample 730. The soil sample 730 is able to be transported securely within the sample tube 710, for example to a laboratory for testing the contents of the tube 710. \| [0059] Referring to Figure 8, an embodiment of the enhanced soil core moisture process 800 will now be described. \| [0060] In a first step 810, the soil sample in the sample tube is received 810. Typically this will be in a laboratory-setting with equipment to analyse the contents of the sample tube. \| [0061] In a second step 820, the soil sample tube has at least one lid removed and the open side of the tube is placed in a bath of sterilised distilled water. In this embodiment, each sample is saturated in 60ml of sterilised distilled water. \| [0062] In this embodiment, 60ml of sterilised distilled water should be sufficient for the soil sample size (using a 5cm diameter and 5cm deep cylinder) not to dilute the “signal” being analysed when testing the water extracted at the end of the process of this embodiment. \| [0063] In this embodiment, de-ionised water or very pure water is not used to prevent the soil leaching some of its contents into the bath of water (which will alter the subsequent analysis data detrimentally). In some embodiments, artificial rainwater can be used. \| [0064] In a third step 830, the sample tube is left for 24 hours at 2-4 degrees Celsius to saturate with the sterilised distilled water. \| [0065] In a fourth step 840, the sample tube is removed from the bath of water in order to allow free drainage of any water that hasn’t soaked into the soil sample in the tube. \| [0066] In a fifth step 850, the sample is placed into a centrifuge and spun for thirty minutes at 1 ,000 revolutions per minute in order to extract the water from the soil sample. The water is collected by the equipment. Typically about 20-30ml will be collected from each soil sample. \| [0067] In a sixth step 860, the water collected by the centrifuge is filtered for five to ten minutes. This filtered water can then be processed as would a normal pore water sample where the soil sample contains sufficient moisture. The filtration aims to remove for example small pieces of soil. In some embodiments, the filtration step could occur earlier by for example placing filter paper at at least one (or both) sides of the cylinder containing the soil sample. \| [0068] Measurements in this embodiment are then taken of alkalinity, pH and EC. In some embodiments, any or any combination of the following measurements as follows can be taken: pH using a benchtop pH meter; EC using a benchtop EC meter; alkalinity using titration using 0.1 M HCL; cations using ICP-AES; anions using IC. \| [0069] After centrifugation and pore water extraction, the core/soil samples are considered ‘spent’. Optionally, in some embodiments, the 'spent cores' are then slowly air dried in an ovenbefore being crushed, mixed and sieved in preparation for an ammonium acetate leach. In an embodiment, 2g of the dried soil is combined with ammonium acetate solution (in this embodiment, analytical grade NH4OAc ammonium acetate is used, with a formula weight of 77.08g/mol) before being placed into a rotating shaker for 2 hours at room temperature. The sample is then centrifuged in either 15ml or 50ml centrifuge tubes for 10 minutes at 4000 RPM before being allowed to settle for 10 mins. The solution is extracted and filtered before being acidified with nitric acid (in this embodiment, analytical grade HNO3 nitric acid, with a formula weight of 63.01 g/mol, is used). The filtered and acidified solution is sent to analysis by ICP- MS. This method allows a quantification of total cations held on the soil exchange sites. \| [0070] In the example embodiment, the ammonium acetate solution comprises a mixture of analytical grade ammonium acetate (NH4OAc; Formula weight = 77.08 g/mol); analytical grade ammonium hydroxide (NH4OH; Formula weight = 35.04 g/mol); analytical grade acetic acid (CH3COOH; Formula weight = 60.05 g/mol); and ultra-high purity water. The ammonium acetate and ultra-high purity water are mixed first, to create a 1M solution. The pH of the solution is then measured in order to then adjust the pH of the solution to pH8.5, by either adding acetic acid to lower the pH or by adding ammonium hydroxide to raise the pH of the solution. \| [0071] In some embodiments, a moisture probe can be used in the soil to be sample prior to take soil core samples and the data from the moisture probe can be used to determine how much water should be contained in the water bath in order to determine how much the pore water sample is diluted by the saturation step in process 800. \| [0072] In some embodiments, in place of a centrifuge, a mechanical pressure device can be used such as a hydraulic press. \| [0073] Any system feature as described herein may also be provided as a method feature, and vice versa. As used herein, means plus function features may be expressed alternatively in terms of their corresponding structure. \| [0074] Any feature in one aspect may be applied to other aspects, in any appropriate combination. In particular, method aspects may be applied to system aspects, and vice versa. Furthermore, any, some and/or all features in one aspect can be applied to any, some and/or all features in any other aspect, in any appropriate combination. \| [0075] It should also be appreciated that particular combinations of the various features described and defined in any aspects can be implemented and/or supplied and/or used independently.	(WO2025/133560)\|[0001] ENHANCED WEATHERING CARBON DIOXIDE REMOVAL QUANTIFICATION METHOD AND APPARATUS \| [0002] Field \| [0003] The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore soil water. \| [0004] Background \| [0005] Enhanced weathering is the process of spreading suitable crushed silicate rock materials over suitable land, such as farmland. Suitable rock materials include rock such as basalt, which naturally reacts with dissolved carbon dioxide in the form of carbonic acid to remove the carbon dioxide from the environment. By crushing the rock, the crushed rock has a larger surface area per particle which speeds up the process of capturing carbon dioxide by increasing the reaction surface area. By spreading the rock over, for example, farmland, carbon dioxide can be captured over a large land surface. \| [0006] During enhanced weathering, it is important to measure the properties of the enhanced weathering reaction in order to measure the amount of carbon dioxide captured in the soil, rivers and eventually oceans. This data can be used to compare against modelled carbon capture, verify carbon credits, or plan further enhanced weathering based on weathering performance. \| [0007] To measure enhanced weathering, one of the measurement options is to extract pore water using a tool called a macro rhyzon in order to determine the level of carbon capture from the sample or samples is obtained. However, when the soil has a low moisture content, it is difficult to extract enough moisture from the soil to get reliable data. \| [0008] Summary of Invention \| [0009] Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. \| [0010] According to a first aspect, there is provided method of obtaining pore water samples from a soil sample (800) comprising: placing the soil sample in a bath of water (820); removingthe soil sample from the bath of water (830); applying pressure to the soil sample to extract at least some water content from the soil sample (850). \| [0011] By allowing the soil sample to be placed in water, the soil sample can saturate with water and this can allow the subsequent removal of both the added water and the original water content for subsequent testing. This can allow the testing of water in a soil sample containing substantially too low a moisture content to provide sufficient water for normal pore water testing. \| [0012] Optionally, the soil sample is contained in a sample tube. Optionally, the sample tube is substantially made from metal and/or is substantially cylindrical. Optionally, the sample tube comprises one or more caps, the one or more caps operable to seal the contents of the sample tube. \| [0013] The soil sample can be contained in a variety of configurations of sample apparatus, but can typically be obtained using a configuration of sample apparatus that is operable to work with a standard centrifuge and/or standard configuration of mechanical pressure apparatus. \| [0014] Optionally, the bath of water comprises a bath of sterilised distilled water. \| [0015] In other embodiments, artificial rainwater can be used. Using sterilised distilled water and/or artificial rainwater can allow the extracted water content to retain substantially all of the properties desired to be measured. \| [0016] Optionally, the step of placing the soil sample in a bath of water comprising placing the soil sample in the bath of water for substantially 24 hours and/or at substantially 2 to 4 degrees Celsius. \| [0017] Placing the soil sample in a bath of water under substantially these conditions can allow the soil sample to saturate with the water contained in the bath and/or substantially not change the properties of the soil sample and/or its water content. \| [0018] Optionally, the step of removing the soil sample from the bath of water comprising removing the soil sample from the bath of water for sufficient duration to allow free drainage. \| [0019] Removing the soil sample from the bath of water can allow only water that has been absorbed by the soil sample to remain prior to further step of the process being performed. \| [0020] Optionally, the step of applying pressure to the soil sample comprises placing the soil sample in a centrifuge. \| [0021] Placing the soil sample in a centrifuge can remove the moisture content of the soil substantially quickly, and/or causes water molecules being removed from the soil sample during the centrifuge operation to pull neighbouring water molecules out of the soil sample. \| [0022] Optionally, the centrifuge spins the soil sample for substantially 30 minutes and/or at substantially 1 ,000 revolutions per minute.Using this configuration of centrifuge equipment can allow sufficient water to be removed from the soil sample to allow subsequent tests to be performed on a substantially sufficient sample size. \| [0023] Optionally, the method further comprises the step of filtering the extracted water content. Optionally, the step of filtering is performed for substantially 5 to 10 minutes. \| [0024] By filtering the water, debris such as soil can be removed which might otherwise impact the measurements/analysis performed on the extracted water. \| [0025] Optionally, the method further comprises drying the soil sample to create a dried soil sample; combining the dried soil sample with an ammonium acetate solution to create a spent core solution; applying pressure to the spent core solution; filtering the spent core solution to remove a treated dried soil sample; further treating the treated dried soil sample with an acid to create an acidified dried soil sample; and analysing the acidified dried soil sample to determine a measurement of cations in the acidified dried soil sample. Optionally drying the soil sample comprising drying the soil sample in an oven and optionally crushing and/or mixing and/or sieving the soil sample to create the dried soil sample. Optionally, the method further comprises the step of placing the dried soil sample in a rotating shaking apparatus. Optionally applying pressure to the spent core solution comprises using a centrifuge apparatus to centrifuge the spent core solution. Optionally the acid is nitric acid. Optionally, the ammonium acetate solution comprises any combination of: ammonium acetate; ammonium hydroxide; and ultra-high purity water. \| [0026] By treating the “spent core” samples using ammonium acetate solution and analysing the treated spent cores, it is possible to measure the cations in the spent core and therefore at the site from which the core was obtained. \| [0027] Brief Description of Drawings \| [0028] Embodiments will now be described, by way of example only and with reference to the accompanying drawings having like-reference numerals, in which: \| [0029] Figure 1 shows an example enhanced weathering process; \| [0030] Figure 2 shows an example of a soil core sample container; \| [0031] Figure 3 shows an example of the use of the soil core sample container, prior to insertion into the soil to be sampled; \| [0032] Figure 4 shows an example of the use of the soil core sample container to insert into the soil to be sampled; \| [0033] Figure 5 shows an example of the use of the soil core sample container being removed from the soil to be sampled;Figure 6 shows an example of the use of the soil core sample container to contain the soil to be sampled; \| [0034] Figure 7 shows an example of the use of the soil core sample container being secured for transport with the soil sample inside; and \| [0035] Figure 8 shows an embodiment of the enhanced soil core moisture process. \| [0036] Specific Description \| [0037] Referring to Figure 1 , an example of an enhanced weathering process 100 will now be described. \| [0038] Enhanced weathering is performed by adding crushed rock 130 to farmland 140. In this described embodiment, the crushed rock 130 is added using farm machinery 120 such as a tractor with a trailer containing the crushed rock 130, where the trailer is configured to disperse the crushed rock 130 in a predetermined dispersal rate over substantially all of the surface of the farmland 140 as the farm machinery 120 travels along the farmland 140, typically travelling along parallel lines back and forth along the farmland 140. \| [0039] Not all of the land needs to be subject to enhanced weathering, so in this embodiment farmland 140 undergoes the enhanced weathering process 100 but non-weathered land 110 does not have any crushed rock 130 spread over its surface. \| [0040] In this embodiment, the properties of the farmland 140 that is to be subject to the enhanced weathering process 100 are determined in advance based on a combination of data for the area in which the farmland 140 is located along with data collected from the farmland 140. This data includes expected rainfall, pH, soil composition. Other data that is used as part of the process 100 is data pertaining to the crushed rock 130, including geochemical properties of the crushed rock and the range of surface area of the rock particles. Using this data, the amount of crushed rock 130 to spread over the farmland 140 and the density of spread/amount to be spread over the farmland 140 is calculated in advance of the spreading operation by the farm machinery 120. \| [0041] In other embodiments, different data can be obtained in advance of the spreading operation. In other embodiments, a spreading plan can comprise different arrangements for different parts of the farmland 140, for example differing amounts of rock to be spread on different portions of the farmland 140. In other embodiments, different equipment can be used to spread the crushed rock 130. In other embodiments, multiple spreading operations may be performed at one or more time intervals. In other embodiments, sensors can be used to monitor the properties of the farmland 140, before and/or after the one or more spreading operations being performed.Following the enhanced weathering operation 100, carbon dioxide is absorbed from the atmosphere above the farmland 140 by a chemical reaction between the dissolved carbon dioxide and the crushed rock 130 spread over the surface of the farmland 140. This captures and sequesters carbon dioxide from the atmosphere into the soil over substantially the entire area that has been subject to enhanced weathering operations 100. Depending on the parameters that have been calculated for the rock spreading operation(s), the rate of carbon dioxide capture depends on the amount and properties of the crushed rock 130 that has been spread over the farmland 140 and a prediction for this carbon dioxide capture will be determined from the calculated parameters for the rock spreading operation(s). \| [0042] Following the enhanced weathering operation 100, one of the measurements that needs to be performed to verify the amount of carbon captured is to measure the properties of the water in the soil, specifically the pore water. Pore water measurements can be key to understanding the soil chemistry and therefore how much carbon dioxide has been removed from the atmosphere. Enhanced weathering performance can depend on the pore water leaving the soil via the normal channels (e.g. streams and rivers) and reaching the ocean. Therefore, operators of enhanced weathering processes typically measure the contents of water in fields undergoing enhanced weathering to demonstrate bicarbonate and cation content in the pore water, which then leaves the soil and in time enters the ocean. \| [0043] Should the soil contain too little moisture, for example in circumstances where there has been little rainfall (e.g. when there has been a droughtfor a number of months), it becomes difficult to extract enough water from a soil sample to conduct normal tests of the pore water. If this is the case then the following process can be used to obtain sufficient water from soil that contains too little moisture. \| [0044] Pore water samples also should be analysed within around 36 hours of taking the sample, as the partial pressure of carbon dioxide in soil is different to that in air, so over time there is outgassing and degradation of the data (e.g. the bicarbonates in the soil sample will typically degrade over time as the pressure equilibrium moves from that of soil to that of air) that can be obtained from the pore water if tests aren’t performed promptly. \| [0045] Simply applying a large degree of pressure to the soil samples may not be possible is the moisture content is too low, as there is a limit to the amount of mechanical suction/pressure that is possible and depending on the type of soil it becomes impossible to extract sufficient water once the moisture levels drop below a certain level (this level varies by soil composition). Some methods of suction/pressure can extract sufficient water from soil samples but take too long, and after 36 hours from taking the soil sample the water extracted doesn’t provide a representative sample for analysis. \| [0046] Referring to Figure 2, an example soil core sample container 200 will now be described.The sample tube 220 is a hollow metal cylinder, which has two caps or lids, a top lid 210 and a bottom lid 230. The top and bottom lids 210, 230 are designed to fit on to the open ends of the tube 220 to secure and seal the sample soil contained within the sample tube 220. In this embodiment the caps 210, 230 fit to the ends of the tube 220 by an interference fit. In other embodiments, the caps 210, 230 can use a screw thread to fit to the tube 220. In other embodiments, other fixing mechanisms can be used to secure the lids 210, 230 to the tube 220. In this embodiment, each cylinder has a 5cm diameter and is 5cm deep. \| [0047] Typically, in this embodiment, multiple samples will be taken each with separate soil core sample containers, commensurate to the area of land being sampled. \| [0048] Referring to Figure 3, an example of use 300 of the soil core container of Figure 2 will now be described. \| [0049] A sample tube 310 (as described above in relation to Figure 2) is shown in this embodiment without caps. It is positioned above the surface of the soil 320. The intention is to sample a core of soil by inserting the sample tube 310 into the soil surface 320 to obtain a core of soil within the sample tube 310. \| [0050] Referring to Figure 4, an example of soil sampling 400 using the soil core container of Figure 2 will now be described. \| [0051] The sample tube 410 is inserted 440 into the soil, penetrating the soil surface 420 and thereby causing a sample of soil 430 to enter into the sample tube 410. In this embodiment, the tube 410 is hammered into the soil. \| [0052] Referring to Figure 5, an example of soil sample removal 500 using the soil core container of Figure 2 will now be described. \| [0053] The sample tube 510 is removed 540 from the soil surface 520, leaving a hole 550 and with the soil sample 530 contained within the sample tube 510. The soil sample 530 typically stays within the sample tube 510 when it is removed from the ground. It is typically very important to keep the soil core as a solid undisturbed soil sample hence it is kept intact within the cylinder 510. \| [0054] Referring to Figure 6, an example of securing the soil 600 within the soil core container of Figure 2 will now be described. \| [0055] The sample tube 610 containing the soil sample 630 then has the two lids 620, 640 placed at either open end of the cylinder 610 containing the soil sample 630. \| [0056] The top lid 620 is fit over one end of the sample tube 610 using an interference fit. The bottom lid 640 is fit over the other end of the sample tube 610 using an interference fit. The lids 620, 640 prevent the soil or any moisture from leaving the interior of the sample tube 610. \| [0057] In other embodiments, other fastening mechanisms can be used to fasten the lids 620, 640 to the tube 610.Referring to Figure 7, an example of readying the soil sample for transport 700 using the soil core container of Figure 2 will now be described. \| [0058] The sample tube 710 is shown with both lids 720, 740 securely fastened over either open end of the cylinder 710 containing the soil sample 730. The soil sample 730 is able to be transported securely within the sample tube 710, for example to a laboratory for testing the contents of the tube 710. \| [0059] Referring to Figure 8, an embodiment of the enhanced soil core moisture process 800 will now be described. \| [0060] In a first step 810, the soil sample in the sample tube is received 810. Typically this will be in a laboratory-setting with equipment to analyse the contents of the sample tube. \| [0061] In a second step 820, the soil sample tube has at least one lid removed and the open side of the tube is placed in a bath of sterilised distilled water. In this embodiment, each sample is saturated in 60ml of sterilised distilled water. \| [0062] In this embodiment, 60ml of sterilised distilled water should be sufficient for the soil sample size (using a 5cm diameter and 5cm deep cylinder) not to dilute the “signal” being analysed when testing the water extracted at the end of the process of this embodiment. \| [0063] In this embodiment, de-ionised water or very pure water is not used to prevent the soil leaching some of its contents into the bath of water (which will alter the subsequent analysis data detrimentally). In some embodiments, artificial rainwater can be used. \| [0064] In a third step 830, the sample tube is left for 24 hours at 2-4 degrees Celsius to saturate with the sterilised distilled water. \| [0065] In a fourth step 840, the sample tube is removed from the bath of water in order to allow free drainage of any water that hasn’t soaked into the soil sample in the tube. \| [0066] In a fifth step 850, the sample is placed into a centrifuge and spun for thirty minutes at 1 ,000 revolutions per minute in order to extract the water from the soil sample. The water is collected by the equipment. Typically about 20-30ml will be collected from each soil sample. \| [0067] In a sixth step 860, the water collected by the centrifuge is filtered for five to ten minutes. This filtered water can then be processed as would a normal pore water sample where the soil sample contains sufficient moisture. The filtration aims to remove for example small pieces of soil. In some embodiments, the filtration step could occur earlier by for example placing filter paper at at least one (or both) sides of the cylinder containing the soil sample. \| [0068] Measurements in this embodiment are then taken of alkalinity, pH and EC. In some embodiments, any or any combination of the following measurements as follows can be taken: pH using a benchtop pH meter; EC using a benchtop EC meter; alkalinity using titration using 0.1 M HCL; cations using ICP-AES; anions using IC. \| [0069] After centrifugation and pore water extraction, the core/soil samples are considered ‘spent’. Optionally, in some embodiments, the 'spent cores' are then slowly air dried in an ovenbefore being crushed, mixed and sieved in preparation for an ammonium acetate leach. In an embodiment, 2g of the dried soil is combined with ammonium acetate solution (in this embodiment, analytical grade NH4OAc ammonium acetate is used, with a formula weight of 77.08g/mol) before being placed into a rotating shaker for 2 hours at room temperature. The sample is then centrifuged in either 15ml or 50ml centrifuge tubes for 10 minutes at 4000 RPM before being allowed to settle for 10 mins. The solution is extracted and filtered before being acidified with nitric acid (in this embodiment, analytical grade HNO3 nitric acid, with a formula weight of 63.01 g/mol, is used). The filtered and acidified solution is sent to analysis by ICP- MS. This method allows a quantification of total cations held on the soil exchange sites. \| [0070] In the example embodiment, the ammonium acetate solution comprises a mixture of analytical grade ammonium acetate (NH4OAc; Formula weight = 77.08 g/mol); analytical grade ammonium hydroxide (NH4OH; Formula weight = 35.04 g/mol); analytical grade acetic acid (CH3COOH; Formula weight = 60.05 g/mol); and ultra-high purity water. The ammonium acetate and ultra-high purity water are mixed first, to create a 1M solution. The pH of the solution is then measured in order to then adjust the pH of the solution to pH8.5, by either adding acetic acid to lower the pH or by adding ammonium hydroxide to raise the pH of the solution. \| [0071] In some embodiments, a moisture probe can be used in the soil to be sample prior to take soil core samples and the data from the moisture probe can be used to determine how much water should be contained in the water bath in order to determine how much the pore water sample is diluted by the saturation step in process 800. \| [0072] In some embodiments, in place of a centrifuge, a mechanical pressure device can be used such as a hydraulic press. \| [0073] Any system feature as described herein may also be provided as a method feature, and vice versa. As used herein, means plus function features may be expressed alternatively in terms of their corresponding structure. \| [0074] Any feature in one aspect may be applied to other aspects, in any appropriate combination. In particular, method aspects may be applied to system aspects, and vice versa. Furthermore, any, some and/or all features in one aspect can be applied to any, some and/or all features in any other aspect, in any appropriate combination. \| [0075] It should also be appreciated that particular combinations of the various features described and defined in any aspects can be implemented and/or supplied and/or used independently.	Family Number\|(108540136)\|108540136\|Object of Invention\|(GB2636853 A)\|The present invention relates to methods of quantifying carbon dioxide removal when performing enhanced weathering operations. \|(WO2025133560 A1)\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. \|Abstract\|(GB2636853 A)\|A method for quantifying carbon dioxide removal when performing enhance weathering operations. Measurements are enabled by taking soil cores 810, placing the core sample into a water bath, 820, leave sample to saturate 830, drain sample 840, apply pressure on the sample 850 to allow a pore sample of water to be extracted from the soil sample 860. Filtering may be carried out on the pore water sample during collection. Thus, pore water samples may be extracted from soil that may not have enough moisture to extract a sufficiently large enough pore sample. The method may then be used to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal. Enhanced weathering is a process of spreading suitable crushed silicate rock materials over land such as farmland enabling carbon dioxide to be captured over a large area.\|(WO2025133560 A1)\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water. Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal.\|Title\|(GB202319995 D0)\|Enhanced weathering carbon dioxide removal quantification method and apparatus\|(GB2636853 A)\|Enhanced weathering carbon dioxide removal quantification method and apparatus\|(WO2025133560 A1)\|Enhanced weathering carbon dioxide removal quantification method and apparatus\|	Analysis of biological materials	G01N-001/28\|G01N-033/24\|G01N-033/24/6		G01N-001/28\|G01N-033/24\|G01N-033/24/6	G01N-001/28\|G01N-033/24	G01N-001/28\|G01N-033/24					US20120103077\|CN115307977\|CN112525630\|CN203772616U	US20120103077 44414932 WHO=Examiner SELF=N CAT=A\|CN115307977 102493973 WHO=Examiner SELF=N\|CN112525630 93215294 WHO=Examiner SELF=N\|CN203772616U 67217407 WHO=Examiner SELF=N		XP091560179; XP086002247; US20120103077; XP037697290\|CN203772616U; CN115307977; CN112525630	(WO2025/133560)\|International Search Report [Examiner]\|-DAVID J BEERLING ET AL: "Enhanced weathering in the U.S. Corn Belt delivers carbon removal with agronomic benefits", ARXIV.ORG, CORNELL UNIVERSITY LIBRARY, 201 OLIN LIBRARY CORNELL UNIVERSITY ITHACA, NY 14853, 6 July 2023 (2023-07-06), XP091560179\|-LOZANO J C ET AL: "A system for obtaining soil solution extracts and soil water retention curves using a bench centrifuge with fixed angle rotors", GEODERMA, ELSEVIER, AMSTERDAM, NL, vol. 361, 27 November 2019 (2019-11-27), XP086002247, ISSN: 0016-7061, [retrieved on 20191127], DOI: 10.1016/J.GEODERMA.2019.114063\|-LAUKKANEN JOHANNA ET AL: "In situ remediation of metal(loid)-contaminated lake sediments with alkali-activated blast furnace slag granule amendment: A field experiment", JOURNAL OF SOILS AND SEDIMENTS, SPRINGER, DE, vol. 22, no. 3, 26 January 2022 (2022-01-26), pages 1054 - 1067, XP037697290, ISSN: 1439-0108, [retrieved on 20220126], DOI: 10.1007/S11368-022-03140-Z\|\|	PENDING	(WO2025/133560)\|PENDING\|(GB2636853)\|PENDING	ALIVE	(WO2025/133560)\|ALIVE\|(GB2636853)\|ALIVE	(WO2025/133560)\|LEGAL DETAILS FOR WO2025/133560\|Actual or expected expiration date=2027-06-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-07-08\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOGB2024/051780\|Application date=2024-07-08\|Standardized application number=2024WO-GB51780\|Event publication date=2025-06-26\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/133560\|Publication stage code=A1\|Publication date=2025-06-26\|Standardized publication number=WO2025133560\|Event publication date=2025-11-06\|Event code=WO/DPE1\|Event group=Examination events\|Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2044-07-08\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP24743471\|Event publication date=2025-08-06\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|(GB2636853)\|LEGAL DETAILS FOR GB2636853\|Actual or expected expiration date=2043-12-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-12-22\|Event code=GB/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=GB GB202319995\|Application date=2023-12-22\|Standardized application number=2023GB-0019995\|Event publication date=2024-02-07\|Event code=GB/D0\|Event indicator=Pos\|Event group=Examination events\|Patent application filed\|Publication country=GB\|Publication number=GB202319995\|Publication stage code=D0\|Publication date=2024-02-07\|Standardized publication number=GB202319995\|Event publication date=2025-07-02\|Event code=GB/A\|Event group=Examination events\|Published Application\|Publication country=GB\|Publication number=GB2636853\|Publication stage code=A\|Publication date=2025-07-02\|Standardized publication number=GB2636853	(WO2025/133560)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/133560)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/133560)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/133560)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/133560)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(WO2025/133560)\|WO; EP\|(GB2636853)\|GB	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=icjTorqguCAiwlzxUQ66p90P/F2Pwh1EkaV0SMUACwOCCKReMmHu7M9Ry4MrhQjLALkMBz8hwaI=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006802716&ekey=2486&xpn=WO2025133560&kind=A1	http://www.wipo.int/patentscope/search/en/detail.jsf?docId=WO2025133560&redirectedID=true	https://permalink.orbit.com/RenderStaticFirstPage?XPN=OThLP3Yvv2mkh5CpoqtjpbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	GB	(WO2025/133560)\|GB	(WO2025/133560)\|NAME=UNDO CARBON LTD 3rd Floor 86-90 Paul Street London, EC2A 4NE , COUNTRY=GB	(WO2025/133560)\|GB	(WO2025/133560)\|NAME=BARNES IP LIMITED Castle Hill House 12 Castle Hill Windsor Berkshire SL4 1PD , POSTCODE=SL4 1PD , COUNTRY=GB	(WO2025/133560)\|GB\|	(WO2025/133560)\|NAME=LIU, Xinran c/o Undo Carbon Ltd 3rd Floor 86-90 Paul Street London Greater London EC2A 4NE, POSTCODE=EC2A 4NE, COUNTRY=GB\|(GB2636853)\|NAME=Xinran Liu	(WO2025/133560)\|8\|(GB2636853)\|8	1	2					(WO2025/133560)\|Number of Claims: NCL=17\|Extended kind: EXTK=x\|\|(GB2636853)\|Number of Claims: NCL=11\|\|(GB202319995)\|Gazette date: GAZDATE=2024-02-07\|		(WO2025/133560)\|ENGLISH (ENG)	(GB2636853)\|Patent\|(WO2025133560)\|Patent\|(GB202319995)\|Patent	Titre: (WO2025/133560)\|Enhanced weathering carbon dioxide removal quantification method and apparatus Résumé: (WO2025/133560)\|The present invention relates to methods of quantifying carbon dioxide removal and related factors/changes when performing enhanced weathering operations. More particularly, the present invention relates to enabling measurements to be taken from soil cores of enhanced weathering products by extracting pore water. Aspects and/or embodiments seek to provide a method to extract sufficient pore water samples from soil, even when the soil has a low moisture content, in order to perform measurements on the pore water, for example to verify or measure enhanced weathering for the purpose of the quantification of carbon dioxide removal.	11	Abstract	gpt-4o-mini	yes	The article focuses on enhanced weathering methods for quantifying carbon dioxide removal, which is central to the topic of accelerated weathering and carbon sequestration.
16	AU2007900853	ZA200906476\|ZA200906474	ZA200906476\|ZA200906474	65403466	ZA200906476 B 2010-09-29 [ZA200906476]\|ZA200906474 B 2010-07-28 [ZA200906474]	2007-02-20	2009-09-17\|2009-09-17	2010-09-29\|2010-07-28	(ZA200906476)\|2010-09-29\|(ZA200906474)\|2010-07-28	(ZA200906476)\|2029-09-17\|(ZA200906474)\|2029-09-17	(ZA200906476)\|System, apparatus and method for carbon dioxide sequestration	(ZA200906476)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From CN101641145 A)	HUNWICK RICHARD J\|HUNWICK RICHARD J	(ZA200906476)\|HUNWICK, RICHARD J\|(ZA200906474)\|HUNWICK, RICHARD J	HUNWICK RICHARD J	(ZA200906476)\|HUNWICK, RICHARD J									Family Number\|(65403466)\|65403466\|Abstract\|(ZA200906474 B)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From CN101641145 A)\|(ZA200906476 B)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From CN101641145 A)\|Title\|(ZA200906474 B)\|System, apparatus and method for carbon dioxide sequestration\|(ZA200906476 B)\|System, apparatus and method for carbon dioxide sequestration\|	Chemical engineering\|Materials, metallurgy	Y02A-050/20\|Y02P-020/151		Y02A-050/20\|Y02P-020/151	B01D\|C01B\|C01B-032/50\|C01B-032/60	B01D\|C01B\|C01B-032/50\|C01B-032/60										GRANTED	(ZA200906476)\|GRANTED\|(ZA200906474)\|GRANTED	ALIVE	(ZA200906476)\|ALIVE\|(ZA200906474)\|ALIVE	(ZA200906476)\|LEGAL DETAILS FOR ZA200906476\|Actual or expected expiration date=2029-09-17\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2009-09-17\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA200906476\|Application date=2009-09-17\|Standardized application number=2009ZA-0006476\|Event publication date=2010-09-29\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA200906476\|Publication stage code=B\|Publication date=2010-09-29\|Standardized publication number=ZA200906476\|(ZA200906474)\|LEGAL DETAILS FOR ZA200906474\|Actual or expected expiration date=2029-09-17\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2009-09-17\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA200906474\|Application date=2009-09-17\|Standardized application number=2009ZA-0006474\|Event publication date=2010-07-28\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA200906474\|Publication stage code=B\|Publication date=2010-07-28\|Standardized publication number=ZA200906474		(ZA200906476)\|ZA\|(ZA200906474)\|ZA	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=U29pnpjL83VLPRBewy3fiKQ6hYovoTT3WeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1			https://permalink.orbit.com/RenderStaticFirstPage?XPN=pwVavdhX2CHvfTygFXo9u5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	AU						(ZA200906476)\|NAME=HUNWICK, RICHARD J\|(ZA200906474)\|NAME=HUNWICK, RICHARD J		1	2								(ZA200906476)\|Patent\|(ZA200906474)\|Patent	Titre: (ZA200906476)\|System, apparatus and method for carbon dioxide sequestration Résumé: (ZA200906476)\|A carbon dioxide sequestration process includes the following steps. In a first stage, a slurry of a metal silicate rock is mixed with ammonia so as to produce a ammonia/water/metal silicate slurry. In a second stage, the process includes scrubbing a gas stream containing carbon dioxide with the solution from the first stage to thereby absorb the carbon dioxide into a reactive slurry. In a third stage, the reactive slurry from the second stage is passed through a reactor that is controlled so as to promote the reaction between the carbon dioxide and the metal silicate to thereby produce a metal carbonate.(From CN101641145 A)	13	Abstract	gpt-4o-mini	yes	The process described involves the use of metal silicate rocks to capture CO₂ and produce metal carbonates, which aligns with the topic of enhanced weathering and carbon sequestration.
17	US63/449,791P\|US63/449,791\|WOUS2024/018316	WOUS2024/018316\|JP2025551726\|EP24767679\|KR10-2025-7033809\|AU2024233973\|CA3288102	JP2026510743\|EP4676898\|KR10-2025-0164234\|AU2024233973\|CA3288102\|WO2024/186724	111402698	WO2024/186724 A1 2024-09-12 [WO2024186724]\|JP2026510743 A 2026-04-10 [JP2026510743]\|EP4676898 A1 2026-01-14 [EP4676898]\|KR10-2025-0164234 A 2025-11-24 [KR20250164234]\|AU2024233973 A1 2025-10-23 [AU2024233973]\|CA3288102 A1 2024-09-12 [CA3288102]	2023-03-03\|2024-03-04	2024-03-04\|2024-03-04\|2024-03-04\|2024-03-04\|2024-03-04\|2024-03-04	2026-04-10\|2026-01-14\|2025-11-24\|2025-10-23\|2024-09-12\|2024-09-12		(EP4676898)\|2044-03-04\|(WO2024/186724)\|2026-09-03\|(JP2026510743)\|2044-03-04\|(KR10-2025-0164234)\|2044-03-04\|(AU2024233973)\|2044-03-04\|(CA3288102)\|2044-03-04	(EP4676898)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide	(EP4676898)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.	DARTMOUTH COLLEGE	(EP4676898)\|Trustees of Dartmouth College ([US])\|(WO2024/186724)\|TRUSTEES OF DARTMOUTH COLLEGE ([US])\|(JP2026510743)\|Trustees of Dartmouth College\|(KR10-2025-0164234)\|TRUSTEES OF DARTMOUTH COLLEGE ([US])\|(AU2024233973)\|TRUSTEES OF DARTMOUTH COLLEGE\|(CA3288102)\|TRUSTEES OF DARTMOUTH COLLEGE ([US])	SHARMA MUKUL\|MORRISON BRIAN	(EP4676898)\|SHARMA, Mukul\|MORRISON, Brian	(EP4676898)\|Maiwald GmbH;Engineering ([DE])\|Reg. Nb: 101782373\|(WO2024/186724)\|AMINI, Farhang ([US])\|(JP2026510743)\|YAMAMOTO Osamu\|Reg. Nb: 100118902\|MIYAMAE,Toru\|Reg. Nb: 100106208\|MATSUO JUNICHI\|Reg. Nb: 100196508\|NAKAMURA MITSUTOSHI\|Reg. Nb: 100126985\|(KR10-2025-0164234)\|KIM, JIN HOI\|KIM, TAE HONG\|(AU2024233973)\|PHILLIPS ORMONDE FITZPATRICK ([AU])\|(CA3288102)\|MBM INTELLECTUAL PROPERTY AGENCY ([CA])\|Reg. Nb: e61a1630-b292-4706-b91c-f3098c8c5df7	(WO2024/186724)\|In some embodiments, the methods of the present disclosure also improve the quality of the soil.\|This process is not only beneficial for managing organic matter in the surface and overall grass health, but also will allow basalt sands to penetrate deeper into the surface of the green.\|Ideally, the material should have no particles greater than 1.0 mm in diameter given the difficulty in getting these larger particles to work down into the turf canopy.\|These costs and methods to spread the products for ERW would be especially difficult in places where this spreading is not common practice.\|	(WO2024/186724)\|1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt sand captures the CO2.\|21. A method of modifying a surface, said method comprising: applying a composition comprising at least one basalt sand to the surface, wherein the at least one basalt sand is in the form of crushed particles.\|39. A modified surface, wherein the modified surface comprises a composition, wherein the composition comprises at least one basalt sand, wherein the at least one basalt sand is in the form of crushed particles.\|	(WO2024/186724)\|In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand that is in the form of crushed particles.\|In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand.\|	(WO2024/186724)\|BASALT SAND(100,66)\|SURFACE MODIFICATION(100,36)\|CO2(100,27)\|ENVIRONMENT(100,16)\|CARBON DIOXIDE(100,8)\|TURF MANAGEMENT(100,4)\|ATMOSPHERIC CARBON DIOXIDE(100,1)\|INTEGRATING ENHANCED ROCK(100,1)\|CRUSHED PARTICLE(67,7)\|HOLYOKE BASALT(62,22)\|BASALT(51,69)\|TURF CANOPY(43,1)\|BURNER BASALT(40,13)\|MANAGED TURF(37,10)\|BLUE RIDGE BASALT(32,7)\|GROUND LAYER(25,16)\|ACTINOMYCES(22,5)\|SUBDIVISION(21,6)\|CAAL2SI2O(20,6)\|MICROBE(20,5)\|PYROXENE(19,8)\|HIGHWAY(19,6)\|NAALSI3O(19,6)\|THOLEIITE(18,10)\|GOLF COURSE ADDITIVE(18,7)\|QUARTZ TOP SAND(18,7)\|SPORTS FACILITY(18,6)\|BACTERIA(18,5)\|MANAGING ORGANIC MATTER(18,1)\|PEAT MOSS(17,7)\|SILICATE(17,5)\|ALKALI ION(17,2)\|YARD(16,6)\|PARK(15,6)\|FUNGUS(15,5)\|HEALTH(14,1)\|SURFACE ACRE(13,39)\|LIME(13,8)\|BICARBONATE HCO3(11,2)\|CRUSHED BASALT SAND PARTICLE(11,2)\|PRETREATED BASALT SAND(11,2)\|LARGE PARTICLE(11,1)\|OUTER LAYER(9,25)\|RESIDENTIAL FIELD(9,6)\|CO2 CAPTURE REACTION(9,5)\|CRUSHED BASALT TON(9,1)\|MAFIC APHANITIC VOLCANIC ROCK(9,1)\|PIONEER VALLEY BASALT(9,1)\|ULTRAFINE PARTICLE(8,3)\|USGA ACCREDITED GOLF COURSE(8,3)\|BASALT INTEGRATION(8,2)\|FULL ROOTZONE BASALT(8,2)\|SOIL FERTILIZER(8,2)\|ARTIFICIAL TOPSOIL CREATION(8,1)\|BASALT AMENDED SOIL COLUMN(8,1)\|BASALT SAND DEPLOYMENT(8,1)\|PURCHASED ROCK(7,2)\|MICROSCOPIC PLAGIOCLASE FELDSPAR(7,1)\|GOLF TURF GRASS STUDY(6,1)\|LEVERHULME INSTITUTE(6,1)\|QUICKBIRD IMAGERY(6,1)\|SAND CUSTOM BLEND(6,1)\|SEQUESTRATION OPPORTUNITY(6,1)\|URBAN SUBURBAN LANDSCAPE(6,1)\|USGA RECOMMENDATION(6,1)\|ENHANCED ROCK WEATHERING(5,12)\|FINE GRAINED PARTICLE(5,3)\|CAPTURED CO2(5,2)\|CAPTURING CO2(5,2)\|ENHANCED CO2 CAPTURE(5,2)\|ROCK DUST LOCAL(5,2)\|USGA ROOT ZONE(5,2)\|AGRICULTURAL FARM(5,1)\|AGRICULTURAL SPREADER(5,1)\|ARXIV PREPRINT(5,1)\|BASALT METRIC TON(5,1)\|CACO3 PRECIPITATION(5,1)\|CO2 CONSUMPTION ASSESSMENT(5,1)\|COMMON PRACTICE(5,1)\|EFFLUENT ALKALINITY(5,1)\|EXCHANGEABLE CALCIUM(5,1)\|FINE GRAINED BASALT SAND(5,1)\|MAXIMIZE SEQUESTRATION(5,1)\|MINE TAILING(5,1)\|ROOTZONE SAND(5,1)\|AGRICULTURAL FIELD(4,6)\|HTTP(4,6)\|COURSE GRAINED PARTICLE(4,3)\|MAXIMUM ENHANCED WEATHERING CO2(4,3)\|MEDIUM PARTICLE(4,3)\|MICROPARTICLE(4,3)\|NANOPARTICLE(4,3)\|NUMEROUS LIMITATION(4,3)\|ENHANCED SOIL HEALTH(4,2)\|NONCRYSTALLINE(4,2)\|SOIL FERTILITY ENHANCEMENT(4,2)\|VISIBLE CRYSTAL(4,2)\|AGRICULTURAL ADDITIVE(4,1)\|AGRONOMIC BENEFIT(4,1)\|ANNUAL CAPTURE(4,1)\|APPROVED GREEN ROOTZONE CONSTRUCTION(4,1)\|BASAL SAND(4,1)\|BASALT POWDER RELEASE(4,1)\|CACO3 PRECIPITATE(4,1)\|CAPTURE POTENTIAL ESTIMATE(4,1)\|CIVILIZATION STABILITY(4,1)\|CO2 METRIC TON(4,1)\|CO2 SEQUESTRATION STRATEGY(4,1)\|CO2 SEQUESTRATION TON ACRE(4,1)\|COARSE FRACTION(4,1)\|COARSE PARTICLE(4,1)\|COARSE SAND(4,1)\|CUSTOM BLENDING(4,1)\|DILUTE BASALT(4,1)\|DRAINAGE PIPE(4,1)\|ELUTION EXPERIMENT(4,1)\|EMPIRICAL MONITORING(4,1)\|ESTIMATED CO2 SEQUESTRATION(4,1)\|EXPERIMENT REPORT(4,1)\|EXPERIMENTAL SETUP(4,1)\|FILTERING BASALT(4,1)\|FREQUENT IRRIGATION(4,1)\|GOLF COURSE ANNUAL SAND(4,1)\|MAJOR GEOLOGIC PROVINCE(4,1)\|NATURAL TOPSOIL(4,1)\|REERSHEMIUS PAPER(4,1)\|ROCK POWDER(4,1)\|ROUNDED ESTIMATE(4,1)\|SEA FLOOR(4,1)\|SOIL ADDITIVE(4,1)\|SOIL SAMPLING(4,1)\|SPECIALIZED SPREADING EQUIPMENT(4,1)\|US TON ACRE(4,1)\|VISIBLE PLAGIOCLASE FELDSPAR(4,1)\|WARM CLIMATE(4,1)\|SOIL QUALITY(3,7)\|SUPRA(3,4)\|SOILS(3,3)\|BASALT SAND PARTICLE SIZE(3,2)\|INSULATION(3,2)\|KG CO2(3,2)\|PERIDOTITE(3,2)\|SOIL NUTRIENT(3,2)\|SPRINKLING(3,2)\|AERATION EQUIPMENT(3,1)\|ANGULAR SAND(3,1)\|ATMOSPHERIC CO2 NET REMOVAL(3,1)\|BACKFILL HOLE(3,1)\|BASALT ENHANCED TOP SANDING(3,1)\|BIORAD COLUMN(3,1)\|CO2 SEQUESTRATION POTENTIAL(3,1)\|ENHANCED ROCK WEATHERING RATE(3,1)\|FAIRWAY TOP SANDING(3,1)\|FINE FRACTION(3,1)\|GOLF COURSE SAND SPREADING(3,1)\|HOT CLIMATE(3,1)\|MONITORING SOIL HEALTH(3,1)\|NATIVE ENVIRONMENT(3,1)\|NEGATIVE EMISSION(3,1)\|REDUCING CO2 EMISSION(3,1)\|SOIL UPPER ROOTZONE(3,1)\|STABLE CACO3(3,1)\|FEO(2,3)\|INTEGRATION(2,3)\|ADOPTION(2,1)\|ADSORPTION(2,1)\|AIRSTREAM(2,1)\|ATMOSPHERIC CARBON(2,1)\|BACKFILLING(2,1)\|BASALT WEATHERING(2,1)\|CONSTANT ATTENTION(2,1)\|CONTINENT(2,1)\|COURSE PARTICLE(2,1)\|CROPLAND(2,1)\|DENSE ROOT ZONE(2,1)\|DISTINCTION(2,1)\|ESTABLISHMENT PERIOD(2,1)\|EXPERIMENT TOTAL DURATION(2,1)\|FINE SAND FRACTION(2,1)\|FOUNDATION(2,1)\|FREQUENT TOP BENEFIT(2,1)\|FULL AERATION(2,1)\|\|(JP2026510743)\|BASALT SAND(100,75)\|ACCELERATION(100,3)\|TURF MANAGEMENT(100,3)\|ATMOSPHERIC CARBON DIOXIDE(100,1)\|ROCK INTEGRATION(100,1)\|HOLYOKE BASALT(63,20)\|PULVERIZED BASALT SAND(55,1)\|BURNER BASALT(45,10)\|BLUE RIDGE BASALT(40,6)\|CRUSHED PARTICLE(38,2)\|BASALT(33,58)\|TURF CANOPY(32,1)\|ADDITIVE(31,20)\|ACTINOMYCETE(29,5)\|ERW CDR(28,2)\|MICROORGANISM(27,5)\|PLAGIOCLASE(26,6)\|BIOCHAR(25,5)\|ARTIFICIAL TOPSOIL(25,2)\|PARTICLE PULVERIZATION(24,2)\|BACTERIA(23,5)\|NATURAL TOPSOIL(23,1)\|GROUND(22,30)\|SILICATE(22,5)\|CARBON DIOXIDE CAPTURE(22,2)\|FELDSPAR(21,8)\|PYROXIN(21,8)\|SOLEITE(21,8)\|PEAT MOSS(21,7)\|QUARTZ TOP SAND(21,7)\|FUNGUS(20,5)\|GROUND LAYER(18,16)\|EXCIPIENT(18,3)\|PARTICULATE(18,1)\|LIME(16,8)\|CONCESSION(16,6)\|CAAL2SI2O(15,5)\|CONTROLLED TURF(15,4)\|ENTIRE LAWN(15,1)\|MINERAL NUTRIENT(15,1)\|NUMEROUS LIMITATION(15,1)\|THOLEIITE(15,1)\|NAALSI3O(14,7)\|TOP SAND(13,20)\|GARDEN(13,6)\|HIGHWAY(13,6)\|SPORTS FACILITY(13,6)\|HEALTH(13,1)\|ORGANIC MATTER HEALTH(13,1)\|PHOSPHORUS(13,1)\|GOLF COURSE(12,36)\|ALKALI ION(12,2)\|PERIDOTITE(12,2)\|SURFACE MODIFICATION(11,48)\|PARK(11,6)\|TAILING(11,2)\|NUTRIENT(10,5)\|PIONEER VALLEY BASALT(10,2)\|FARMLAND(10,1)\|SLAG(9,2)\|OUTER LAYER(8,25)\|GRIND BASALT SAND(8,2)\|PRETREATED BASALT SAND(8,2)\|LARGE PARTICLE(8,1)\|AGRICULTURAL LAND(7,5)\|BICARBONATE(7,3)\|ERW(7,3)\|RESIDENTIAL AREA(6,6)\|ROOT ZONE BASALT(6,6)\|CO2 CAPTURE REACTION(6,4)\|COARSE PARTICULATE(6,4)\|MANAGED TURF(6,3)\|USGA CERTIFIED GOLF COURSE(6,3)\|PULVERIZED BASALT(6,2)\|SOIL FERTILIZER(6,2)\|MAFIC AMORPHOUS VOLCANIC ROCK(6,1)\|ROCK WEATHERING PROMOTION INTRODUCTION(6,1)\|BASALT POWDER(5,3)\|ULTRAFINE PARTICULATE(5,2)\|AGRICULTURAL DUSTING(5,1)\|BASALT SAND INTRODUCTION(5,1)\|ERW FEASIBILITY(5,1)\|GROUND BASALT INTRODUCING TON(5,1)\|LAWN NUTRITIONAL BENEFIT(5,1)\|QUICKBIRD IMAGERY(5,1)\|SLOW WEATHERING KINETICS(5,1)\|URBAN SUBURBAN LANDSCAPE(5,1)\|USGA RECOMMENDATION(5,1)\|ORGANIC MATTER(4,5)\|COARSE PARTICLE(4,2)\|ROCK DUST LOCAL(4,2)\|ARXIV PREPRINT(4,1)\|ERW STRATEGY(4,1)\|EXCHANGEABLE CALCIUM(4,1)\|FINE GRAINED BASALT SAND(4,1)\|USGA RECOMMENDED ROOT REGION(4,1)\|INCORPORATION(3,8)\|BASALT ENHANCED TOP SANDING(3,3)\|GOLF COURSE CERTIFICATION(3,3)\|NANOPARTICLE(3,3)\|ENHANCED SOIL HEALTH(3,2)\|MICROPARTICULATE(3,2)\|ROCK POWDER(3,2)\|SOIL FERTILITY ENHANCEMENT(3,2)\|SOIL PH OPTIMIZATION(3,2)\|AGRICULTURAL ADDITIVE(3,1)\|AGRONOMIC BENEFIT(3,1)\|ANNUAL COURSE SANDING(3,1)\|ARTIFICIAL TOPSOIL FORMATION(3,1)\|BASALT CONSUMPTION(3,1)\|BASALT INTRODUCTION(3,1)\|CAPTURE POTENTIAL ESTIMATE(3,1)\|CITED DOCUMENT(3,1)\|CIVILIZATION STABILITY(3,1)\|COARSE FRACTION(3,1)\|DILUTE BASALT(3,1)\|DISASTER CLASS IMPACT(3,1)\|EMPIRICAL MONITORING(3,1)\|FILTERING BASALT(3,1)\|FREQUENT IRRIGATION(3,1)\|FUNDAMENTAL THREAT(3,1)\|GOLF TURF(3,1)\|HEALTH MONITORING(3,1)\|ISOLATION STRATEGY(3,1)\|LABORATORY EXPERIMENT(3,1)\|MAXIMIZE ISOLATION(3,1)\|PREEXISTING SUB SOIL(3,1)\|REPORTER ASSAY(3,1)\|ROCK INCORPORATION(3,1)\|ROUGH SAND(3,1)\|ROUGHNESS PARTICLE(3,1)\|ROUNDED ESTIMATE(3,1)\|SEA FLOOR(3,1)\|SOIL ADDITIVE(3,1)\|SOIL SAMPLING(3,1)\|SOILS PH(3,1)\|TON INTRODUCTION(3,1)\|TURF ROOT REGION(3,1)\|US TON ACRE(3,1)\|SOIL QUALITY(2,7)\|SURFACE SOIL(2,6)\|HTTP(2,5)\|AERATION(2,3)\|GRINDING(2,3)\|GROUND SURFACE(2,3)\|NAKED EYE(2,3)\|AL2SI2O(2,2)\|GOLF COURSE ADDITIVE(2,2)\|MEDIUM PARTICULATE(2,2)\|METRIC TON(2,2)\|SCIENTIFIC LITERATURE(2,2)\|SOIL NUTRIENT(2,2)\|SPRINKLING(2,2)\|ULTRAFINE PARTICLE(2,2)\|ANGULAR SAND(2,1)\|BASALT MODIFIED SOIL(2,1)\|DISCLOSURE CAPTURE(2,1)\|ENHANCED ROCK WEATHERING RATE(2,1)\|ERWS COST(2,1)\|FAIRWAY TOP SANDING(2,1)\|FINE FRACTION(2,1)\|GOLF COURSE SAND SPRAYING(2,1)\|HOT CLIMATE(2,1)\|MAINTAINING PRODUCTIVITY(2,1)\|NET ATMOSPHERE(2,1)\|PERIODIC CARE(2,1)\|PLAGIOCLASE FELDSPAR(2,1)\|SIMULATION(2,1)\|STABLE CACO(2,1)\|TOP SANDING ADOPTION(2,1)\|2H4SIO(1,1)\|ACCESSORY(1,1)\|ADSORPTION(1,1)\|ALKALINITY(1,1)\|ASSESSMENT(1,1)\|ATMOSPHERIC CARBON(1,1)\|BASALT CHEMICAL COMPOSITION(1,1)\|BASALT CURRENT(1,1)\|BASALT SAND PARTICLE SIZE(1,1)\|CLIMATE CHANGE IMPACT(1,1)\|\|(KR10-2025-0164234)\|BASALT SAND(100,54)\|CARBON DIOXIDE(100,8)\|LAWN MANAGEMENT(100,3)\|STRENGTHENING INTEGRATION(100,1)\|CRUSHED PARTICLE(72,7)\|BASALT SAND CAPTURE(67,1)\|HOLYOAK BASALT(61,19)\|BASALT(46,80)\|LAWN CANOPY(41,1)\|BERTNER BASALT(35,8)\|BLUE RIDGE BASALT(32,7)\|GRASS(28,32)\|GROUND LAYER(25,16)\|BURNER BASALT(24,2)\|ACTINOMYCETE(23,5)\|MICROORGANISM(23,4)\|SPARGING PRODUCT(22,1)\|SPARGING(21,1)\|PARCEL(20,3)\|NAALSI3O(19,6)\|LITHOGRAPH(19,2)\|FARMLAND(18,7)\|GOLF COURSE ADDITIVE(18,7)\|SPORTS FACILITY(18,6)\|BACTERIA(18,5)\|PEAT MOSS(18,5)\|QUARTZ TOP SAND(17,7)\|ALKALI ION(17,2)\|HIGHWAY(16,6)\|SILICATE(16,5)\|SURFACE MODIFICATION(15,38)\|FUNGUS(15,5)\|PLAGIOCLASE FELDSPAR(15,2)\|ERWS(15,1)\|PARK(14,6)\|YARD(14,6)\|SOLEITE(14,5)\|LIME(13,7)\|PRETREATED BASALT SAND(11,2)\|PYROXENE(11,2)\|LARGE PARTICLE(11,1)\|OUTER LAYER(10,23)\|COARSE PARTICLE(10,7)\|ACRE TON SURFACE(10,2)\|CRUSHED BASALT INJECTING TON(10,1)\|BICARBONATE(9,3)\|BUTTNER BASALT(9,3)\|HAYLOOK BASALT(9,2)\|ATMOSPHERIC CO2(9,1)\|HOLYOAK BASALT RIDGE(9,1)\|MAFIC APLASTIC VOLCANIC ROCK(9,1)\|PIONEER VALLEY BASALT(9,1)\|MANAGED TURF(8,3)\|USGA CERTIFIED GOLF COURSE(8,3)\|ARTIFICIAL TOPSOIL CREATION(8,1)\|COMMINUTED BASALT SAND PARTICLE(8,1)\|INTEGRATING BASALT SAND(8,1)\|ANNUAL SURFACE ACRE(7,21)\|RESIDENTIAL AREA(7,6)\|BASALT POWDER(7,3)\|GRIND BASALT SAND(7,1)\|STRENGTHENING ROCK INTEGRATION(7,1)\|SURFACE TON ACRE(7,1)\|PETE MOSS(6,2)\|PURCHASED ROCK(6,2)\|ERW CDR(6,1)\|ERW FEASIBILITY(6,1)\|MAJOR GEOLOGICAL GEOGRAPHY(6,1)\|QUICKBIRD IMAGERY(6,1)\|SAND CUSTOM BLEND(6,1)\|SLOW WEATHERING KINETICS(6,1)\|TOPSOIL ROOTZONE(6,1)\|URBAN SUBURBAN LANDSCAPE(6,1)\|USGA RECOMMENDATION(6,1)\|CAPTURE REACTION(5,5)\|GOLF COURSE CERTIFICATION(5,4)\|ULTRAFINE PARTICLE(5,3)\|LIMITATION CAAL2SI2O(5,2)\|ROCK DUST LOCAL(5,2)\|ROCK POWDER(5,2)\|AGRICULTURAL SPRAYER(5,1)\|ARXIV PREPRINT(5,1)\|BASALT METRIC TON(5,1)\|CACO PRECIPITATION(5,1)\|EFFLUENT ALKALINITY(5,1)\|ERW STRATEGY(5,1)\|EXCHANGEABLE CALCIUM(5,1)\|FINE BASALT SAND(5,1)\|FULL ROOTZONE BASALT(5,1)\|GROUND BASALT SAND PARTICLE(5,1)\|HOLIOKE BASALT(5,1)\|MANAGED GRASS(5,1)\|MAXIMIZE SEQUESTRATION(5,1)\|PORE BACKFILLING(5,1)\|SAND USAGE ESTIMATE(5,1)\|SOIL FERTILIZER(5,1)\|HTTP(4,6)\|MEDIUM PARTICLE(4,3)\|MICROPARTICLE(4,3)\|NANOPARTICLE(4,3)\|VISIBLE CRYSTAL(4,2)\|AGRICULTURAL ADDITIVE(4,1)\|AGRONOMIC BENEFIT(4,1)\|CAPTURE CO2(4,1)\|CIVILIZATION STABILITY(4,1)\|COARSE GRAINED PARTICLE(4,1)\|COARSE SAND(4,1)\|CUSTOM BLENDING(4,1)\|DILUTE BASALT(4,1)\|ELUTION EXPERIMENT(4,1)\|EMPIRICAL MONITORING(4,1)\|FACILITY INFRASTRUCTURE(4,1)\|FILTERING BASALT(4,1)\|FINE SANDSTONE(4,1)\|FREQUENT IRRIGATION(4,1)\|GOLF LAWN GRASS(4,1)\|GOLF TURF(4,1)\|GRASS MANAGEMENT(4,1)\|GRAY STONE(4,1)\|ISOLATION STRATEGY(4,1)\|LABORATORY EXPERIMENT(4,1)\|MANAGED LAWN(4,1)\|NATURAL TOPSOIL(4,1)\|REERSHEMIUS PAPER(4,1)\|ROUNDED ESTIMATE(4,1)\|SOIL ADDITIVE(4,1)\|SOIL SAMPLING(4,1)\|SPECIALIZED SPRAY EQUIPMENT(4,1)\|TON INJECTION(4,1)\|US TON ACRE(4,1)\|VISIBLE SANDSTONE(4,1)\|SPRAYING(3,5)\|BASALT SAND PARTICLE SIZE(3,2)\|GUIDANCE(3,2)\|NORTH(3,2)\|PERIDOTITE(3,2)\|AERATION EQUIPMENT(3,1)\|ANGLED SAND(3,1)\|ANNUAL FULL COURSE SANDING(3,1)\|BASALT ENHANCED TOP SANDING(3,1)\|BIORAD COLUMN(3,1)\|ENHANCED ROCK WEATHERING RATE(3,1)\|ENTIRE PLANTING LAYER BASALT(3,1)\|EXPERIMENT TOTAL DURATION(3,1)\|FAIRWAY TOP SANDING(3,1)\|FINE GRAINED PARTICLE(3,1)\|GUIDELINE(3,1)\|HOT CLIMATE(3,1)\|MAXIMUM REINFORCEMENT(3,1)\|MONITORING SOIL HEALTH(3,1)\|NEGATIVE EMISSION(3,1)\|PLANT BED(3,1)\|SIMULATION(3,1)\|SOIL COLUMN(3,1)\|SPREADING EQUIPMENT(3,1)\|STABLE CACO(3,1)\|ULTRAFINE RATIO(3,1)\|UNIFORM MODULUS(3,1)\|FEO(2,3)\|GRINDING(2,3)\|INTEGRATION(2,3)\|ADSORPTION(2,1)\|ASSESSMENT(2,1)\|BASALT WEATHERING(2,1)\|CO2 REMOVAL(2,1)\|COARSE RATIO(2,1)\|COMBINING REACTION(2,1)\|COMMINUTING(2,1)\|COMMINUTION(2,1)\|CONTINENT(2,1)\|DISTINCTION(2,1)\|DRAINPIPE(2,1)\|\|(AU2024233973)\|BASALT SAND(100,58)\|HOLYOKE BASALT(61,21)\|CRUSHED PARTICLE(54,5)\|BASALT(45,60)\|TURF CANOPY(42,1)\|BURNER BASALT(39,12)\|MANAGED TURF(36,10)\|BLUE RIDGE BASALT(33,6)\|GROUND LAYER(25,16)\|SUBDIVISION(21,6)\|ACTINOMYCES(21,5)\|PYROXENE(19,7)\|HIGHWAY(19,6)\|CAAL2SI(19,5)\|MICROBE(19,5)\|CO2(18,18)\|THOLEIITE(18,9)\|GOLF COURSE ADDITIVE(18,7)\|QUARTZ TOP SAND(18,7)\|SPORTS FACILITY(18,6)\|BACTERIA(18,5)\|NAALSI(18,5)\|PEAT MOSS(17,7)\|ALKALI ION(17,2)\|MANAGING ORGANIC MATTER(17,1)\|YARD(16,6)\|SILICATE(16,5)\|SURFACE MODIFICATION(15,34)\|PARK(15,6)\|FUNGUS(15,5)\|SURFACE ACRE(13,39)\|LIME(13,8)\|HEALTH(13,1)\|REGULAR TOPSANDING AERATION(11,2)\|LARGE PARTICLE(11,1)\|OUTER LAYER(9,23)\|RESIDENTIAL FIELD(9,6)\|BICARBONATE(9,3)\|MAFIC APHANITIC VOLCANIC ROCK(9,1)\|PIONEER VALLEY BASALT(9,1)\|CO2 CAPTURE REACTION(8,4)\|USGA ACCREDITED GOLF COURSE(8,3)\|BASALT INTEGRATION(8,2)\|FULL ROOTZONE BASALT(8,2)\|SOIL FERTILIZER(8,2)\|ARTIFICIAL TOPSOIL CREATION(8,1)\|BASALT AMENDED SOIL COLUMN(8,1)\|BASALT SAND DEPLOYMENT(8,1)\|CRUSHED BASALT SAND PARTICLE(8,1)\|CRUSHED BASALT TON(8,1)\|PRETREATED BASALT SAND(8,1)\|CARBON DIOXIDE(7,4)\|COARSE GRAVEL FINE GRAVEL(7,1)\|COARSE SAND COARSE SAND(7,1)\|MICROSCOPIC PLAGIOCLASE FELDSPAR(7,1)\|PURCHASED ROCK(6,2)\|ULTRAFINE PARTICLE(6,2)\|GOLF TURF GRASS STUDY(6,1)\|LEVERHULME INSTITUTE(6,1)\|QUICKBIRD IMAGERY(6,1)\|SAND CUSTOM BLEND(6,1)\|SEQUESTRATION OPPORTUNITY(6,1)\|URBAN SUBURBAN LANDSCAPE(6,1)\|USGA RECOMMENDATION(6,1)\|ENHANCED ROCK WEATHERING(5,12)\|CAPTURED CO2(5,2)\|CAPTURING CO2(5,2)\|ENHANCED CO2 CAPTURE(5,2)\|ROCK DUST LOCAL(5,2)\|USGA ROOT ZONE(5,2)\|AGRICULTURAL FARM(5,1)\|AGRICULTURAL SPREADER(5,1)\|ARXIV PREPRINT(5,1)\|BACKFILL AERATION(5,1)\|BASALT METRIC TON(5,1)\|BASALT TON YEAR(5,1)\|CACO3 PRECIPITATION(5,1)\|CLAY ROOTZONE(5,1)\|CO2 CONSUMPTION ASSESSMENT(5,1)\|COMMON PRACTICE(5,1)\|EFFLUENT ALKALINITY(5,1)\|EXCHANGEABLE CALCIUM(5,1)\|FINE GRAINED BASALT SAND(5,1)\|MAXIMIZE SEQUESTRATION(5,1)\|MINE TAILING(5,1)\|ROOTZONE SAND(5,1)\|SQ FT YEAR EAR(5,1)\|TBASALT CO2 SEQUESTRATION POTENTIAL(5,1)\|UNIFORMITY CLAY COEFFICIENT(5,1)\|AGRICULTURAL FIELD(4,6)\|HTTP(4,6)\|MAXIMUM ENHANCED WEATHERING CO2(4,3)\|TURF MANAGEMENT(4,3)\|ENHANCED SOIL HEALTH(4,2)\|FINE GRAINED PARTICLE(4,2)\|NONCRYSTALLINE(4,2)\|SOIL FERTILITY ENHANCEMENT(4,2)\|VISIBLE CRYSTAL(4,2)\|AGRICULTURAL ADDITIVE(4,1)\|AGRONOMIC BENEFIT(4,1)\|ALKALINITY CO2(4,1)\|ANNUAL CAPTURE(4,1)\|APPROVED GREEN ROOTZONE CONSTRUCTION(4,1)\|BASAL SAND(4,1)\|BASALT POWDER RELEASE(4,1)\|BASALT YEAR METRIC TON(4,1)\|CACO3 PRECIPITATE(4,1)\|CAPTURE POTENTIAL ESTIMATE(4,1)\|CIVILIZATION STABILITY(4,1)\|CO2 METRIC TON(4,1)\|CO2 SEQUESTRATION METRIC TON(4,1)\|CO2 SEQUESTRATION STRATEGY(4,1)\|COARSE FRACTION(4,1)\|COARSE PARTICLE(4,1)\|CUSTOM BLENDING(4,1)\|DILUTE BASALT(4,1)\|DRAINAGE PIPE(4,1)\|ELUTION EXPERIMENT(4,1)\|EMPIRICAL MONITORING(4,1)\|ESTIMATED CO2 SEQUESTRATION(4,1)\|EXPERIMENT REPORT(4,1)\|EXPERIMENTAL SETUP(4,1)\|FILTERING BASALT(4,1)\|FREQUENT IRRIGATION(4,1)\|GOLF COURSE ANNUAL SAND(4,1)\|MAJOR GEOLOGIC PROVINCE(4,1)\|NATURAL TOPSOIL(4,1)\|PLANAV SKY(4,1)\|REERSHEMIUS PAPER(4,1)\|ROCK POWDER(4,1)\|ROOTZONE W INORGANIC AMENDMENT(4,1)\|ROUNDED ESTIMATE(4,1)\|SEA FLOOR(4,1)\|SOIL SAMPLING(4,1)\|SPECIALIZED SPREADING EQUIPMENT(4,1)\|US TON ACRE(4,1)\|VISIBLE PLAGIOCLASE FELDSPAR(4,1)\|WARM CLIMATE(4,1)\|SOIL QUALITY(3,7)\|SUPRA(3,4)\|SOILS(3,3)\|BASALT SAND PARTICLE SIZE(3,2)\|COURSE GRAINED PARTICLE(3,2)\|INSULATION(3,2)\|KG CO2(3,2)\|MEDIUM PARTICLE(3,2)\|MICROPARTICLE(3,2)\|NANOPARTICLE(3,2)\|NUMEROUS LIMITATION(3,2)\|PERIDOTITE(3,2)\|SOIL NUTRIENT(3,2)\|SPRINKLING(3,2)\|AERATION EQUIPMENT(3,1)\|ANGULAR SAND(3,1)\|ATMOSPHERIC CO2 NET REMOVAL(3,1)\|BACKFILL HOLE(3,1)\|BASALT ENHANCED TOP SANDING(3,1)\|BIORAD COLUMN(3,1)\|ENHANCED ROCK WEATHERING RATE(3,1)\|FAIRWAY TOP SANDING(3,1)\|FINE FRACTION(3,1)\|FINE SAND SILT(3,1)\|GOLF COURSE SAND SPREADING(3,1)\|HOT CLIMATE(3,1)\|MONITORING SOIL HEALTH(3,1)\|NATIVE ENVIRONMENT(3,1)\|NEGATIVE EMISSION(3,1)\|REDUCING CO2 EMISSION(3,1)\|SOIL UPPER ROOTZONE(3,1)\|STABLE CACO3(3,1)\|W PEAT SIEVE(3,1)\|INTEGRATION(2,3)\|ADOPTION(2,1)\|ADSORPTION(2,1)\|AIRSTREAM(2,1)\|ATMOSPHERIC CARBON(2,1)\|BACKFILLING(2,1)\|BASALT WEATHERING(2,1)\|CARBON OFFSET PRICE(2,1)\|COMBINING REACTION(2,1)\|CONSTANT ATTENTION(2,1)\|CONTINENT(2,1)\|COURSE PARTICLE(2,1)\|CROPLAND(2,1)\|DENSE ROOT ZONE(2,1)\|DISTINCTION(2,1)\|ESTABLISHMENT PERIOD(2,1)\|EXPERIMENT TOTAL DURATION(2,1)\|FINE SAND FRACTION(2,1)\|FOUNDATION(2,1)\|FREQUENT TOP BENEFIT(2,1)\|FULL AERATION(2,1)\|	(WO2024/186724)\|CLAIMS \|1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt sand captures the CO2.\|2. The method of claim 1, wherein the at least one basalt sand is in purified form.\|3. The method of claim 1, wherein the at least one basalt sand comprises a plurality of different types of basalt sands.\|4. The method of claim 1, wherein the at least one basalt sand is selected from the group consisting of plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalt, or combinations thereof.\|5. The method of claim 1, wherein the at least one basalt sand comprises Holyoke Basalt.\|6. The method of claim 1, wherein the at least one basalt sand comprises a compound selected from the group consisting of CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof.\|7. The method of claim 1, wherein the composition further comprises one or more additives.\|8. The method of claim 7, wherein the one or more additives is selected from the group consisting of silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof.\|9. The method of claim 1, wherein the exposing occurs by applying the composition to a surface.\|10. The method of claim 9, wherein the method further comprises removing an outer layer of the surface prior to applying the composition to the surface.\|11. The method of claim 9, wherein the composition is placed on an outer layer of the surface.\|12. The method of claim 9, wherein the composition is applied at a concentration of at least about 25 ton per acre of the surface per year.\|13. The method of claim 9, wherein the surface comprises soil.\|14. The method of claim 13, wherein the soil is selected from the group consisting of top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof.\|15. The method of claim 13, wherein the soil comprises a soil layer below grass.\|16. The method of claim 9, wherein the surface comprises a field.\|17. The method of claim 16, wherein the field comprises an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof.\|18. The method of claim 16, wherein the field comprises a golf course.\|19. The method of claim 1, wherein the CO2 comprises atmospheric CO2.\|20. The method of claim 1, wherein the CO2 capture occurs by a reaction between the at least one basalt sand, CO2, and water, wherein the reaction releases one or more alkaline ions and mineralized bicarbonate (HCO3-).\|21. A method of modifying a surface, said method comprising: applying a composition comprising at least one basalt sand to the surface, wherein the at least one basalt sand is in the form of crushed particles.\|22. The method of claim 21, wherein the at least one basalt sand is in purified form.\|23. The method of claim 21, wherein the at least one basalt sand comprises a plurality of different types of basalt sands.\|24. The method of claim 21, wherein the at least one basalt sand is selected from the group consisting of plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalt, or combinations thereof.\|25. The method of claim 21, wherein the at least one basalt sand comprises Holyoke Basalt.\|26. The method of claim 21, wherein the at least one basalt sand comprises a compound selected from the group consisting of CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof.\|27. The method of claim 21, wherein the composition further comprises one or more additives.\|28. The method of claim 27, wherein the one or more additives is selected from the group consisting of silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof.\|29. The method of claim 21, wherein the exposing occurs by applying the composition to a surface.\|30. The method of claim 29, wherein the method further comprises removing an outer layer of the surface prior to applying the composition to the surface.\|31. The method of claim 29, wherein the composition is placed on an outer layer of the surface.\|32. The method of claim 29, wherein the composition is applied at a concentration of at least about 25 tons per acre of the surface per year.\|33. The method of claim 29, wherein the surface comprises soil.\|34. The method of claim 33, wherein the soil is selected from the group consisting of top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof.\|35. The method of claim 33, wherein the soil comprises a soil layer below grass.\|36. The method of claim 29, wherein the surface comprises a field.\|37. The method of claim 36, wherein the field comprises an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof.\|38. The method of claim 36, wherein the field comprises a golf course.\|39. A modified surface, wherein the modified surface comprises a composition, wherein the composition comprises at least one basalt sand, wherein the at least one basalt sand is in the form of crushed particles.\|40. The modified surface of claim 39, wherein the at least one basalt sand is in purified form.\|41. The modified surface of claim 39, wherein the at least one basalt sand comprises a plurality of different types of basalt sands.\|42. The modified surface of claim 39, wherein the at least one basalt sand is selected from the group consisting of plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalt, or combinations thereof.\|43. The modified surface of claim 39, wherein the at least one basalt sand comprises Holyoke Basalt.\|44. The modified surface of claim 39, wherein the at least one basalt sand comprises a compound selected from the group consisting of CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof.\|45. The modified surface of claim 39, wherein the composition further comprises one or more additives.\|46. The modified surface of claim 45, wherein the one or more additives is selected from the group consisting of silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof.\|47. The modified surface of claim 39, wherein the composition is positioned on an outer layer of the surface.\|48. The modified surface of claim 39, wherein the composition is at a concentration of at least about 25 tons per acre of the surface.\|49. The modified surface of claim 39, wherein the surface comprises soil.\|50. The modified surface of claim 49, wherein the soil is selected from the group consisting of top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof.\|51. The modified surface of claim 49, wherein the soil comprises a soil layer below grass.\|52. The modified surface of claim 39, wherein the surface is associated with a field.\|53. The modified surface of claim 52, wherein the field comprises an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof.\|54. The modified surface of claim 52, wherein the field comprises a golf course.	(WO2024/186724)\| INTEGRATING ENHANCED ROCK WEATHERING AND TURF MANAGEMENT TO SEQUESTER ATMOSPHERIC CARBON DIOXIDE CROSS-REFERENCE TO RELATED APPLICATIONS \|[0001] The present application claims the benefit of U.S. Provisional Patent Application No. 63/449,791, filed on March 3, 2023. The entirety of the aforementioned application is incorporated herein by reference. BACKGROUND \|[0002] Current methods of capturing carbon dioxide (CO2) have numerous limitations in terms of efficacy, efficiency, costs, and the ability to capture CO2 at a large scale. Numerous embodiments of the present disclosure address the aforementioned limitations. SUMMARY \|[0003] In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand that is in the form of crushed particles. In some embodiments, the basalt sand is in purified form. In some embodiments, the basalt sand includes pre-treated basalt sand. In some embodiments, the basalt sand includes a plurality of different types of basalt sands. In some embodiments, the basalt sands of the present disclosure may be in the form of course particles, medium particles, course- grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. In some embodiments, the basalt sands may be mixed with other sands and/or soil additives. \|[0004] The basalt sands of the present disclosure may include various compounds. For instance, in some embodiments, the compounds may include, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof. In some embodiments, the basalt sand compositions of the present disclosure include, without limitation, plagioclase feldspars-containing basalt, pyroxenes-containing basalt, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof.\|[0005] Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. In some embodiments, the compositions of the present disclosure are placed on an outer layer of the surface. In some embodiments, the methods of the present disclosure may also include a step of removing an outer layer of a surface prior to applying a composition of the present disclosure to the surface. In some embodiments, the methods of the present disclosure also include a step of integrating the compositions of the present disclosure with a surface (e.g., within the topsoil and/or rootzone of a turf). \|[0006] Additional embodiments of the present disclosure pertain to modified surfaces that include a composition of the present disclosure. Further embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure. \|[0007] Additional embodiments of the present disclosure pertain to methods of making the basalt sand compositions of the present disclosure. In some embodiments, such methods include crushing at least one basalt sand such that the crushing results in the formation of crushed basalt sand particles. In some embodiments, the methods of the present disclosure also include a step of isolating, filtering, and/or drying the basalt sand. DESCRIPTION OF THE DRAWINGS \|[0008] FIGS. 1A-1C illustrate an exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a full rootzone basalt sand integration process. \|[0009] FIGS.2A-2B illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a top sand only basalt sand integration process. \|[0010] FIGS.3A-3C illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a basalt enhanced top sanding and aeration process, which can be used as part of ongoing aeration and top sanding programs to form a modified surface. \|[0011] FIGS.4A-4C illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a full rootzone basalt sand integration process.\|[0012] FIG.5 illustrates the locations of top 99 Golf Courses in the United States in relation to three major geologic provinces with basalt. \|[0013] FIG. 6 shows the particle size distribution of Pioneer Valley basalt from Rock Dust Local (rockustlocal.com). \|[0014] FIGS.7A-7B provide an experimental setup (FIG. 7A) and experimental results (FIG.7B) demonstrating that soil amended with basalt powder releases six-times more alkalinity than the control soil. DETAILED DESCRIPTION \|[0015] It is to be understood that both the foregoing general description and the following detailed description are illustrative and explanatory, and are not restrictive of the subject matter, as claimed. In this application, the use of the singular includes the plural, the word “a” or “an” means “at least one”, and the use of “or” means “and/or”, unless specifically stated otherwise. Furthermore, the use of the term “including”, as well as other forms, such as “includes” and “included”, is not limiting. Also, terms such as “element” or “component” encompass both elements or components comprising one unit and elements or components that include more than one unit unless specifically stated otherwise. \|[0016] The section headings used herein are for organizational purposes and are not to be construed as limiting the subject matter described. All documents, or portions of documents, cited in this application, including, but not limited to, patents, patent applications, articles, books, and treatises, are hereby expressly incorporated herein by reference in their entirety for any purpose. In the event that one or more of the incorporated literature and similar materials defines a term in a manner that contradicts the definition of that term in this application, this application controls. \|[0017] Climate change fundamentally threatens the safety and stability of modern civilization. In order to avoid the increasingly disastrous and costly effects of climate change, net atmospheric concentrations of greenhouse gases must be reduced. Such reductions can be achieved through improvements in productive efficiency (e.g., reducing CO2 emissions while maintaining output) and carbon dioxide (CO2) removal (CDR).\|[0018] Enhanced rock weathering (ERW) is an example of a CDR-based approach that aims to take atmospheric Carbon (CO2) out of air and store it as bicarbonate or carbonate. ERW has been investigated in cropland but not in golf courses or other managed turfs. Several different types of materials have been used for ERW, including peridotite, basalt, slag, and mine-tailings. Furthermore, ERW has beneficial effects on soil health by releasing beneficial mineral nutrients into the soil, such as calcium, potassium, phosphorous, and magnesium. \|[0019] However, ERW-based CDR processes utilizing peridotites, mine tailings, slag, and basalt other than tholeiites have numerous limitations. Foremost among them is the potential release of heavy metals to the environment and slow weathering kinetics. Furthermore, manufacturing large amounts of basalt powder (including mining, crushing, sorting, and shipping) can be an energy intensive process. Moreover, there is additional energy required to apply the basalt powder multiple times throughout the growing season with specialized spreading equipment that is typically gas powered. These costs and methods to spread the products for ERW would be especially difficult in places where this spreading is not common practice. This results in increased development costs and increased energy consumption. Such limitations may render ERW-based CDR processes inefficient and impractical for large scale CO2 capture from large surface areas. \|[0020] In comparison, golf course greens and courses at large, which, in general, are intensively managed, already engage in this top sanding process. They own and have the technical expertise to spread large amounts of sand onto the turf surface and rootzone. There are large amounts of research into turf grass and golf course maintenance practices aiding the development and deployment of basalt sands within existing maintenance and construction. Additionally, Golf courses have many characteristics that make them ideal to engender CDR through ERW as they are frequently located in warm and hot climates, are frequently watered and receive precipitation, and have high levels of primary productivity leading to turfs generating large amounts of organic matter—three parameters that increase the weathering rate. \|[0021] In sum, current methods of capturing CO2 have numerous limitations in terms of efficacy, efficiency, costs, and the ability to capture CO2 from large surface areas. Numerous embodiments of the present disclosure address the aforementioned limitations. \|[0022] Basalt sand compositions\|[0023] In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand. Basalt is the name of a mafic aphanitic volcanic rock that includes, without limitation, tholeiites. Basalt is exposed around the world on the continents and at the ocean floor. The basalt sands of the present disclosure may be in various forms. For instance, in some embodiments, the basalt sand is in isolated form (i.e., basalt sand isolated from its native environment). In some embodiments, the basalt sand is in the form of crushed particles. In some embodiments, the basalt sand is in purified form. In some embodiments, the basalt sand includes pre-treated basalt sand. In some embodiments, the basalt sands of the present disclosure may be in the form of course particles, medium particles, course-grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. \|[0024] The basalt sands of the present disclosure may include various compounds. For instance, in some embodiments, the compounds may include, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof. \|[0025] The compositions of the present disclosure may include various types of basalt sands. In some embodiments the basalt sand includes a plurality of different types of basalt sands. In some embodiments, the basalt sand includes, without limitation, plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. \|[0026] In some embodiments, the basalt sand compositions of the present disclosure include plagioclase feldspars-containing basalts and pyroxenes-containing basalts. In some embodiments, the basalt sand compositions of the present disclosure include microscopic or visible plagioclase feldspars-containing basalts and pyroxenes-containing basalts, with little or no olivines, and with minor iron spinel and phosphate. \|[0027] In some embodiments, the basalt sand compositions of the present disclosure include tholeiites. In some embodiments, the basalt sand compositions of the present disclosure include tholeiites with low heavy metal concentrations.\|[0028] In some embodiments, the basalt sand compositions of the present disclosure include Holyoke Basalt. In some embodiments, the Holyoke Basalt is derived from Massachusetts (MA). In some embodiments, the average concentrations of Cr, Ni, Cu, Zn, and Pb in Holyoke Basalt are 13 ppm, 33 ppm, 78 ppm, 86 ppm, and 4 ppm, respectively. In some embodiments, the average concentrations of Cr, Ni, Cu, Zn, and Pb in Holyoke Basalt are 384 ppm, 75 ppm, 145 ppm, 88 ppm, and 1.5 ppm, respectively. In some embodiments, Holyoke Basalt is essentially devoid of visible crystals. In some embodiments, Holyoke Basalt is in non-crystalline form. In some embodiments, Holyoke Basalt includes the following elements: SiO2, TiO2, Al2O3, Fe2O3, FeO, CaO, MgO, MnO, K2O, Na2O, and P2O5. \|[0029] In some embodiments, the basalt sand compositions of the present disclosure include Butner Basalt. In some embodiments, the Butner Basalt is derived from North Carolina (NC). In some embodiments, Butner Basalt is essentially devoid of visible crystals. In some embodiments, Butner Basalt is in non-crystalline form. \|[0030] In some embodiments, Holyoke Basalt and Butner Basalt each include the following elements: SiO2, TiO2, Al2O3, Fe2O3, FeO, CaO, MgO, MnO, K2O, Na2O, and P2O5. In some embodiments, the aforementioned elements are present at average weight percentages listed in Table 1. Table 1. Average weight percentages of major elements of Holyoke and Butner Basalts. The data are averages of published results downloaded from GEOROC.org. () FeO for Butner basalt reflects the total amount of iron present without making a distinction between Fe(II) and Fe(III). (*) EPOT is the maximum enhanced weathering CO2 capture potential in units of kg CO2 t-1 (as defined in Renforth (2019) The negative emission potential of alkaline materials. Nature Comm. https://doi.org/10.1038/s41467-019-09475-5). \|[0031] The basalt sands of the present disclosure may include various particle shapes. For instance, in some embodiments, the basalt sand particles of the present disclosure may be angular or rounded depending on their application. In some embodiments, different proportions of basalt sand particle sizes and blends may be used to best suit the local conditions. For instance, in some embodiments, finer sands may retain more moisture within an upper rootzone of a soil. In some embodiments, such sands may also include reduced moisture content through various treatment methods (e.g., kiln drying) so that they can be applied to a surface more effectively (e.g., more efficient spreading using golf course sand spreading and aeration equipment). \|[0032] The compositions of the present disclosure may also include additional components. For instance, in some embodiments, the compositions of the present disclosure may also include one or more additives. In some embodiments, the one or more additives include, without limitation, silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz- based top sands, lime, or combinations thereof.\|[0033] In some embodiments, the additives include one or more golf course additives. In some embodiments, the golf course additives include, without limitation, peat moss, quartz-based top sands, lime, or combinations thereof. In some embodiments, the quartz-based top sands are utilized to dilute the basalt. In some embodiments, the basalt sand compositions of the present disclosure may be treated with such additives depending on the needs of a surface (e.g., a local soil). \|[0034] Methods of modifying a surface \|[0035] Additional embodiments of the present disclosure pertain to methods of modifying a surface. In some embodiments, such methods include applying a composition of the present disclosure to the surface. Suitable compositions were described supra and are incorporated herein by reference. \|[0036] The compositions of the present disclosure may be applied to surfaces in various manners. For instance, in some embodiments, the compositions of the present disclosure may be applied by methods that include, without limitation, spreading, pouring, sprinkling, spraying, or combinations thereof. In some embodiments, the compositions of the present disclosure are placed on an outer layer of the surface. In some embodiments, the compositions of the present disclosure may become integrated with the surface. In some embodiments, the methods of the present disclosure may also include a step of removing an outer layer of a surface prior to applying a composition of the present disclosure to the surface. \|[0037] FIGS. 1A-1C, 2A-2B, 3A-3C, and 4A-4C illustrate exemplary processes for applying a composition of the present disclosure to a surface. For instance, FIGS.1A-1C illustrate an exemplary process for applying a composition of the present disclosure (i.e., basalt sand 14) to a surface 10 with an outer layer 12. In this example, outer layer 12 is first removed from surface 10 (FIG. 1A). Thereafter, basalt sand 14 is applied to surface 10 (FIG.1B) to form a new outer layer 16 on surface 10, which contains basalt sand 14 (FIG.1C). \|[0038] FIGS.2A-2B show an example of a more specific process to integrate an existing surface (i.e., a top sand 30 of a golf course) with a composition of the present disclosure (i.e., basalt sand 34) to build up a new outer layer 36 where basalt sands 34 are integrated in the top sand 30 of the greens and turf surface generally. As illustrated in FIG.2A, basalt sand 34 is applied to top sand 30 of a golf course with an outer layer (i.e., the grass and rootzone 32). In some embodiments, basalt sand 34 may be applied with agricultural spreaders, such as equipment 35, to top sand 30. As illustrated in FIG. 2B, the application of basalt sands 34 forms a new outer layer 36 on surface 30, which contains composition 34 integrated into surface 30 (FIG.2B). \|[0039] FIGS. 3A-3C show another specific method of integrating the compositions of the present disclosure (i.e., basalt sand 44) into a surface (i.e., a top sand 40 with topsoil 42) by using aeration as a chance to rapidly integrate larger amounts of basalt sands 44 deeper into the root zone of top sand 40. In this Example, equipment 43 is used to punch holes 45 into surface 40 of the grass. In some embodiments, such as process may remove around 10% of the organic matter dense root zone and topsoil 42 (FIGS.3A-3B). Thereafter, the same spreading equipment 43 may be used to backfill holes 45 with basalt sands 44 (FIGS. 3B-3C). This process is not only beneficial for managing organic matter in the surface and overall grass health, but also will allow basalt sands to penetrate deeper into the surface of the green. \|[0040] FIGS. 4A-4C show another specific method to integrate the compositions of the present disclosure (i.e., basalt sands 54) into a surface (i.e., top sand 50 with an outer layer 52). In this example, outer layer 52 is first removed from surface 50 (FIG.4A). Thereafter, composition 54 is applied to surface 50 (FIG.4B) to form a new outer layer 56 on surface 50, which contains composition 54 (FIG. 4C). In some embodiments, this option allows for a large amount of basalt sand to be used as the entire soil profile will be entirely rebuilt and basalt sands can be included in the blend as well as in the sand spread into the rootzone as the grass is regrown.\|[0041] The compositions of the present disclosure may be applied to a surface at various concentrations. For instance, in some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 0.1 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 0.5 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 1 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 2 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 2.5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 7.5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 10 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 25 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 50 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 75 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 100 tons per acre of the surface. \|[0042] The compositions of the present disclosure may be applied to a surface at varying levels of frequency. For instance, in some embodiments, the compositions of the present disclosure may be applied to a surface from one time to twenty times per year. In some embodiments, the compositions of the present disclosure may be applied to a surface from one time to five times per year. \|[0043] In some embodiments, full aeration and backfilling holes of a surface may only be done one to five times per year. Since a larger volume of soil may be removed through aeration, more top sand may be needed during aeration than regular top sanding.\|[0044] The compositions of the present disclosure may be applied to various surfaces. For instance, in some embodiments, the surface is associated with a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. \|[0045] In some embodiments, the field includes managed turf. In some embodiments, the managed turf is in the form of a monoculture. In some embodiments, the managed turf may require constant attention and maintenance as well as a high amount of nutrients and agricultural additives to keep the turf growing consistently. \|[0046] In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course, such as, but not exclusive to the accredited golf courses outlined in FIG.5. \|[0047] In some embodiments, the surface includes a soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0048] In some embodiments, the methods of the present disclosure also improve the quality of the soil. For instance, in some embodiments, the improved soil quality includes at least one of nutrient enhancement, enhanced CO2 capture, enhanced soil fertility, enhanced soil health, optimization of soil pH, or combinations thereof. As an example, soils developed on Holyoke Basalt as well as Blue ridge basalts have higher pH than those developed on surrounding rocks. They are also richer in nutrients, especially exchangeable Ca and Mg than soil. Table 2 compares soil pH, Organic Matter (OM) and cations on soils developed on north and south sides of ridges made of Holyoke Basalt in Massachusetts. Here, the concentrations are in ppm and uncertainties given in parentheses. The soils developed on Holyoke Basalt have low concentrations of heavy metals. Table 2. A comparison of soil pH, Organic Matter (OM) and cations on soils developed on north and south sides of ridges made of Holyoke Basalt in Massachusetts (data is from Karen B. Searcy, Brayton F. Wilson and James H. Fownes, The Journal of the Torrey Botanical Society, 2003, 130 (3), pp.158-169). \|[0049] In some embodiments, the improved soil quality provides various advantages. For instance, in some embodiments, the improved soil quality reduces or eliminates a need for the use of one or more soil nutrients, one or more soil fertilizers, additives (e.g., lime), or combinations thereof. \|[0050] Modified Surfaces \|[0051] Additional embodiments of the present disclosure pertain to modified surfaces. In some embodiments, the modified surfaces of the present disclosure include a composition of the present disclosure. Suitable compositions were described supra and are incorporated herein by reference.\|[0052] The compositions of the present disclosure may be associated with surfaces in various manners. For instance, in some embodiments, the compositions of the present disclosure are positioned on an outer layer of the surface. FIG.1C illustrates an example of a modified surface 20. In this example, modified surface 20 includes surface 10 with an outer layer 16 that contains a composition of the present disclosure 14. FIG.2B illustrates another example of a modified surface 39. In this example, modified surface 39 includes a surface 30 with an outer layer 36. In this example, a composition of the present disclosure 34 is integrated into surface 30 and outer layer 36. FIG.3C illustrates another example of a modified surface 49. In this example, modified surface 49 includes a surface 40 that contains a composition of the present disclosure 44 integrated into the surface. FIG. 4C illustrates another example of a modified surface 60. In this example, modified surface 60 includes a surface 50 with outer layer 56 that contains a composition of the present disclosure 54 integrated into the surface. \|[0053] The modified surfaces of the present disclosure may include various concentrations of the compositions of the present disclosure. For instance, in some embodiments, the composition is at a concentration of at least about 0.1 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 0.5 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 1 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 2 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 2.5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 7.5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 10 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 25 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 50 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 75 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 100 tons per acre of the surface.\|[0054] In some embodiments, the modified surfaces of the present disclosure are associated with a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course. \|[0055] In some embodiments, the modified surfaces of the present disclosure include a soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0056] In some embodiments, the composition improves the quality of the soil. For instance, in some embodiments, the improved soil quality includes at least one of nutrient enhancement, enhanced CO2 capture, enhanced soil fertility, enhanced soil health, optimization of soil pH, or combinations thereof. In some embodiments the improved soil quality reduces or eliminates a need for the use of one or more soil nutrients, one or more soil fertilizers, additives (e.g., lime), or combinations thereof. \|[0057] Methods of CO2 Capture from an Environment \|[0058] Additional embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment. In some embodiments, such methods include exposing the environment to a composition of the present disclosure. Suitable compositions were described supra and are incorporated herein by reference. In some embodiments, the basalt sands in the compositions of the present disclosure capture the CO2. \|[0059] The methods of the present disclosure may be utilized to capture CO2 from various environments. For instance, in some embodiments, the environment includes, without limitation, an airstream, a gas stream, an industrial plant, an atmosphere, ambient air, or combinations thereof. In some embodiments, the environment includes ambient air. \|[0060] Various methods may also be utilized to expose an environment to a composition of the present disclosure. For instance, in some embodiments, the exposing occurs by flowing the environment through the composition. In some embodiments, the exposing occurs by placing the composition at or near the environment.\|[0061] In some embodiments, the exposing occurs by applying the composition to a surface. Various methods may be utilized to apply the compositions of the present disclosure to a surface. For instance, in some embodiments, the application occurs by a method that includes, without limitation, spreading, pouring, sprinkling, spraying, or combinations thereof. \|[0062] In some embodiments, the methods of the present disclosure also include a step of removing an outer layer of a surface prior to applying the composition to the surface. In some embodiments, the composition is placed on an outer layer of the surface. \|[0063] The methods of the present disclosure may capture CO2 from various surfaces. For instance, in some embodiments the surface includes soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0064] In some embodiments, the surface includes a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course. \|[0065] The compositions of the present disclosure may be applied to surfaces at various concentrations for CO2 capture. For instance, in some embodiments, the composition is applied at a concentration of at least about 0.1 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 0.5 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 1 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 2 tons per acre of the surface per year. In some embodiments the composition is applied at a concentration of at least about 2.5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 7.5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 10 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 25 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 50 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 75 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 100 tons per acre of the surface. \|[0066] The methods of the present disclosure may be utilized to capture various types of CO2. For instance, in some embodiments, the captured CO2 includes atmospheric CO2. In some embodiments, the captured CO2 includes CO2 embedded within a surface. \|[0067] Without being bound by theory, CO2 capture may occur by various mechanisms. For instance, in some embodiments, CO2 capture may occur by at least one of sequestration, direct capture, adhesion, binding, adsorption, electrostatic interaction, or combinations thereof. \|[0068] Without being bound by further theory, CO2 capture may occur through various chemical reactions. For instance, in some embodiments, the CO2 capture occurs by a reaction between at least one basalt sand, CO2, and water. In some embodiments, the reaction releases one or more alkaline ions and mineralized bicarbonate (HCO3-). In some embodiments, the reactions combine HCO3- with Ca2+ ions to produce stable CaCO3 mineral.\|[0069] Without being bound by further theory, CO2 capture can occur through various reactions of silicate minerals, CO2, and H2O. For instance, in some embodiments where the basalt sand includesa CO2 capture reaction can occur through the reaction shown in equation 1.\|[0070] In some embodiments where the basalt sand includes NaAlSi3O8, a CO2 capture reaction can occur through the reaction shown in equation 2.\|[0071] In some embodiments where the basalt sand includes (Ca, Mg)2Si2O6, a CO2 capture reaction can occur through the reaction shown in equation 3.\|[0072] In some embodiments where the basalt sand includes (Mg, Fe)2SiO4, a CO2 capture reaction can occur through the reaction shown in equation 4.\|[0073] In some embodiments, atmospheric CO2 removed by a CO2 capture reaction is either retained as a long lived HCO3- or a CaCO3 precipitate. In some embodiments, production of these compounds leads to net removal of atmospheric CO2\|[0074] In some embodiments, Ca2+ and HCO3- react in accordance with equation 5 to result in the precipitation of CaCO3\|[0075] Methods of making basalt sand compositions \|[0076] Additional embodiments of the present disclosure pertain to methods of making the basalt sand compositions of the present disclosure. In some embodiments, such methods include crushing at least one basalt sand such that the crushing results in the formation of crushed basalt sand particles.\|[0077] In some embodiments, the methods of the present disclosure also include a step of isolating, filtering and/or drying the basalt sand. In some embodiments, the methods of the present disclosure include a step of filtering basalt sand based on the particle size of the basalt sand. In some embodiments, the isolating occurs prior to the crushing. In some embodiments, the isolating includes purifying at least one basalt sand. \|[0078] The methods of the present disclosure may be utilized to crush various basalt sands. Suitable basal sands were described supra and are incorporated herein by reference. For instance, in some embodiments, the basalt sands include, without limitation, plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. In some embodiments, at least one basalt sand includes a compound that includes, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4 or combinations thereof. \|[0079] Various methods may be utilized to crush basalt sands. For instance, in some embodiments, the crushing occurs by methods that include, without limitation, grinding, sonicating, pounding, compressing, milling (e.g., ball milling and/or hammer milling), or combinations thereof. In some embodiments, the crushed particles are in the form of fine-grained particles, course particles, medium particles, course-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. \|[0080] In some embodiments, the methods of the present disclosure also include a step of adding one or more additives to the basalt sand compositions. In some embodiments, the one or more additives include, without limitation, silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof. \|[0081] The methods of the present disclosure can have numerous embodiments. For instance, depending on the moisture content of the sands, kilns or other drying methods may be needed to produce spreadable top sand. \|[0082] Additional embodiments \|[0083] Reference will now be made to more specific embodiments of the present disclosure and experimental results that provide support for such embodiments. However, Applicants note that the disclosure below is for illustrative purposes only and is not intended to limit the scope of the claimed subject matter in any way.\|[0084] Example 1. Integrating Enhanced Rock Weathering (ERW) on Golf Courses \|[0085] This Example describes the deployment of enhanced rock weathering (ERW) practices alongside existing turf management programs to demonstrate the viability of ERW as a CO2 sequestration strategy for golf courses. This ERW strategy replaces traditional top sands with basalt sands for CO2 capture. \|[0086] Golf course construction typically entails a combination of subterranean drainage systems, irrigation, and the creation of an artificial topsoil consisting of a mixture of sand and soil to ensure proper drainage from the rootzone and base layer. In many cases, a “push-up green” is built with a custom blend of sand, peat moss (or other organic matter), and other additives. In some cases, a “sand- cap” is built over the existing sub-soil if the permeability is especially low. This is followed by layers of special soil, amended with sand to reduce the concentration of organic material (OM). An artificial topsoil may be necessary if the existing natural topsoil is too thin, lacking in nutrients, and/or over- compacted. Complete green construction guidelines are provided by the “USGA (2018). USGA Recommendations for a Method of Putting Green Construction.” \|[0087] After the topsoil has been created, seeding takes place and the “establishment period” begins. The grass begins to grow and root structures develop. \|[0088] Basalt sands could be integrated into existing golf course management programs. Moreover, when establishing a new course (or fully renovating an old course), designers can account for local conditions when integrating the basalt sands (e.g., climate, soil conditions, drainage, and/or local pests). \|[0089] Basalt sands could be used in laying the foundation for the entire course, incorporating many tons of crushed basalts into the sand-based root zone, and providing nutrient benefits to the surrounding soils and grasses. Additionally, fine-grained basalt sands could be used at multiple points in the development process with especially large quantities used during rootzone construction in addition to top sanding practices. Both cases provide an opportunity to integrate basalts effectively. \|[0090] The integration of basalt sands into the turf management programs at golf courses may bean optimal way to maximize the sequestration potential of golf courses. The highly managed soil structure of managed turf is ideally suited for enhanced rock weathering due to the high net primary productivity of the golf turf (estimated 1,100.5 g Carbon/m2/year), high volume of water flux from frequent irrigation, and existing systems for monitoring soil health, composition, and pH. (Wu, J., & Bauer, M. (2012). Estimating Net Primary Production of Turfgrass in an Urban-Suburban Landscape with QuickBird Imagery. Remote Sensing, Vol. 4, Issue 4, Pp. 849-866, 4, 849–866. https://doi.org/10.3390/rs4040849). \|[0091] This process has the potential to sequester an estimated 26 to 340 metric tons of carbon dioxide per golf course via green top and course wide sanding annually, depending on the integration level. With around 15,000 plus golf courses spread across the United States, this works out to an annual capture of between 391,000 and 5.15 million metric tons of CO2 per year from top dressing alone. \|[0092] These figures are calculated in Table 3. The sand application rates are derived from (Whitlark & Thompson, 2019; USGA Green Section Record, 57(9). https://www.usga.org/content/usga/home- page/course-care/green-section-record/57/9/light-and-frequent-topdressing-programs.html) and the sequestration rate of 20% is a rounded estimate based on current CDR potential figures from scientific literature, such as the basalts used in the Reershemius paper, which shows a capture potential of 183.56 kgCO2 t-1 (18.3%). This paper also discusses a potential method of measuring weathering based on a mass balance approach known as TiCAT. However, there are still questions regarding the effectiveness of this methodology (Reershemius, T., Kelland, M.E., Davis, I.R., D'Ascanio, R., Kalderon-Asael, B., Asael, D., Epihov, D.E., Beerling, D.J., Reinhard, C.T. and Planavsky, N.J., 2023. A new soil-based approach for empirical monitoring of enhanced rock weathering rates. arXiv preprint arXiv:2302.05004.). \|[0093] Additional simulations run on the MatLab weathering model from the Leverhulme Institute provided similar capture potential estimates of between 15-20% when parameters similar to that of a golf course soil profile were used. (Beerling et al., 2020, Nature, 583(7815), 242–248. https://doi.org/10.1038/s41586-020-2448-9; P. Renforth, 2012, International Journal of Greenhouse Gas Control, 10, 229–243). These estimates differ from the results in the lab experiment Applicants conducted using basalts from the Pioneer Valley.\|[0094] Regardless, in order to effectively measure and verify the amount of CO2 captured when basalt sands are deployed in the field, a reliable system of measurement must be developed. This verification process may include a variety of testing at individual courses. Various methods of measurement including, but not exclusive to, soil sampling, testing, other analyses, chemical testing, other laboratory or field-based testing, as well as sampling of water from existing drainage pipes and other sources around the course exist to conduct tests and analysis to verify weathering as well as the amount of CO2 sequestered. \|[0095] Tables 3-4 show the estimated values of carbon captured from golf courses. Calculations: Golf Course Annual Sand Use & CO2 Sequestration Potential EstimateCO2 Sequestration Tons/ Acre/ met. Tons/ hectare/ metric tons of Potential (metricTotal (Greens & Fairways – Combined)Table 3. Sand Use Estimates based on current industry top sand application rates and estimated CO2 Sequestration per golf course annual application. Table 4. Estimated range of value of Carbon Credits per golf course depending on the course integration level in USD($). \|[0096] The integration of basalt sands into the turf management practices of golf courses can be accomplished within existing infrastructure via putting green top sanding and aeration programs or through fairway top sanding. Although fairway top sanding and aeration is less common, recent golf turf grass studies emphasize the benefits of frequent and finer top sand applications to both greens and fairways. The adoption of course-wide top sanding significantly raises the sequestration opportunity to around 340 metric tons of CO2 per year. Depending on the course, basalt sands could also be used during construction or renovation to sequester greater amounts of CO2 once efficacy can be proven. \|[0097] To evaluate the extent to which alkalinity is released from basalt weathering, Applicants purchased rock powder Pioneer Valley basalt from Rock Dust Local (rockustlocal.com). This basalt is nearly identical in its chemical composition to that of Holyoke Basalt and has a maximum enhanced weathering CO2 capture potential of 203 kg CO2 t-1. The rock powder was dried and sieved. The particle size distribution of the rock power is shown in FIG.6.\|[0098] The basalt powder was mixed with sieved and dried soil from Dartmouth Organic Farm in a ratio of 10 g basalt to 170 g soil and packed in a Biorad® column to a height of ~6 cm. The soil used is Windsor loam. It is quite infertile and has not been fertilized. The column area is 23.76 cm2, meaning that the amount of basalt added is equivalent to 19 US ton/acre. As a control, 180 g of the same soil was also packed in columns as shown in FIG.7A. Water passed through the columns was weighed and measured for Na, K, Ca, and Mg. The alkalinity of the solution was also calculated. \|[0099] Experiments conducted over 3 months show that, with reference to the controls, the soil amended with basalt powder releases five-times more alkalinity (FIG. 7B). The data show that the basalt amended soil consumes 1.94 g of CO2 per 10 g of basalt (19.4% consumption) in comparison to soil control. This is equivalent to consumption of 194 kg of CO2 t-1 of basalt and approaches the theoretical maximum enhanced weathering CO2 capture potential for this rock. Additionally, the results are summarized in Table 5.Table 5. Changes in Alkalinity of effluent from basalt amended soil columns with reference to soil controls show that, on average, 19.4% of basalt was weathered over 88 days when 5 different elution experiments were conducted. Due to the time lag between experiments the total duration of experiments was about six months (May 2023-Oct 2023).\|[0100] While Applicants’ assessment of CO2 consumption per metric ton of basalt matches well with that recently reported experiment conducted over 4 years in an agricultural farm in Illinois (Beerling, D.J. et al. (2024) Enhanced weathering in the US Corn Belt delivers carbon removal with agronomic benefits, Proc. Nat. Acad. Sci.,121(9), e2319436121, https://doi.org/10.1073/pnas.2319436121), Applicants expect that the total CO2 consumed would be much higher in the golf courses, reaching the theoretical CO2 capture potential due to high temperatures and higher amounts of organic matter present in soil. \|[0101] Tables 6 and 7 provide general guidelines for top sands and USGA recommended root zones, respectively. Tables 6 and 7 provide recommended particle size distribution for a USGA approved Green rootzone construction, as well as a finer top sand blend that is based on the rootzone sand but with less coarse particles and more fine, ultra-fine, and other small particle sizes. A recent article (Whitlark & Thompson, 2019; USGA Green Section Record, 57(9). https://www.usga.org/content/usga/home-page/course-care/green-section-record/57/9/light-and- frequent-topdressing-programs.html) provided additional guidelines: “A general guideline is to select a sand that has a minimum of 50 percent of its particles in the medium-sized fraction (0.25-0.50 millimeters (mm) in diameter) and 15 to 40 percent in the coarse fraction (0.5-1.0 mm in diameter). The fine sand fraction (0.15-0.25 mm) should not exceed 25 percent, and the very fine fraction (0.05 – 0.15 mm) should not exceed 5 percent. Ideally, the material should have no particles greater than 1.0 mm in diameter given the difficulty in getting these larger particles to work down into the turf canopy. It is recommended to use a material with a coefficient of uniformity (CU) greater than 1.8. If the sand is too narrowly graded, which will produce a low CU, this may result in soft, unstable surfaces. However, the CU is not the only determining factor in stability – sand shape also plays a role, with angular sands being more stable. Utilizing a coarser sand during aeration will create more stability.” \|Typical Top sand GuidelinesTable 6. General guidelines for top sands.Table 7. General guidelines for USGA recommended root zones.\|[0102] Without further elaboration, it is believed that one skilled in the art can, using the description herein, utilize the present disclosure to its fullest extent. The embodiments described herein are to be construed as illustrative and not as constraining the remainder of the disclosure in any way whatsoever. While the embodiments have been shown and described, many variations and modifications thereof can be made by one skilled in the art without departing from the spirit and teachings of the invention. Accordingly, the scope of protection is not limited by the description set out above, but is only limited by the claims, including all equivalents of the subject matter of the claims. The disclosures of all patents, patent applications and publications cited herein are hereby incorporated herein by reference, to the extent that they provide procedural or other details consistent with and supplementary to those set forth herein.	(WO2024/186724)\| INTEGRATING ENHANCED ROCK WEATHERING AND TURF MANAGEMENT TO SEQUESTER ATMOSPHERIC CARBON DIOXIDE CROSS-REFERENCE TO RELATED APPLICATIONS \|[0001] The present application claims the benefit of U.S. Provisional Patent Application No. 63/449,791, filed on March 3, 2023. The entirety of the aforementioned application is incorporated herein by reference. BACKGROUND \|[0002] Current methods of capturing carbon dioxide (CO2) have numerous limitations in terms of efficacy, efficiency, costs, and the ability to capture CO2 at a large scale. Numerous embodiments of the present disclosure address the aforementioned limitations. SUMMARY \|[0003] In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand that is in the form of crushed particles. In some embodiments, the basalt sand is in purified form. In some embodiments, the basalt sand includes pre-treated basalt sand. In some embodiments, the basalt sand includes a plurality of different types of basalt sands. In some embodiments, the basalt sands of the present disclosure may be in the form of course particles, medium particles, course- grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. In some embodiments, the basalt sands may be mixed with other sands and/or soil additives. \|[0004] The basalt sands of the present disclosure may include various compounds. For instance, in some embodiments, the compounds may include, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof. In some embodiments, the basalt sand compositions of the present disclosure include, without limitation, plagioclase feldspars-containing basalt, pyroxenes-containing basalt, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof.\|[0005] Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. In some embodiments, the compositions of the present disclosure are placed on an outer layer of the surface. In some embodiments, the methods of the present disclosure may also include a step of removing an outer layer of a surface prior to applying a composition of the present disclosure to the surface. In some embodiments, the methods of the present disclosure also include a step of integrating the compositions of the present disclosure with a surface (e.g., within the topsoil and/or rootzone of a turf). \|[0006] Additional embodiments of the present disclosure pertain to modified surfaces that include a composition of the present disclosure. Further embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure. \|[0007] Additional embodiments of the present disclosure pertain to methods of making the basalt sand compositions of the present disclosure. In some embodiments, such methods include crushing at least one basalt sand such that the crushing results in the formation of crushed basalt sand particles. In some embodiments, the methods of the present disclosure also include a step of isolating, filtering, and/or drying the basalt sand. DESCRIPTION OF THE DRAWINGS \|[0008] FIGS. 1A-1C illustrate an exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a full rootzone basalt sand integration process. \|[0009] FIGS.2A-2B illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a top sand only basalt sand integration process. \|[0010] FIGS.3A-3C illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a basalt enhanced top sanding and aeration process, which can be used as part of ongoing aeration and top sanding programs to form a modified surface. \|[0011] FIGS.4A-4C illustrate another exemplary process for applying a composition of the present disclosure to a surface to form a modified surface. In some embodiments, such a process is referred to as a full rootzone basalt sand integration process.\|[0012] FIG.5 illustrates the locations of top 99 Golf Courses in the United States in relation to three major geologic provinces with basalt. \|[0013] FIG. 6 shows the particle size distribution of Pioneer Valley basalt from Rock Dust Local (rockustlocal.com). \|[0014] FIGS.7A-7B provide an experimental setup (FIG. 7A) and experimental results (FIG.7B) demonstrating that soil amended with basalt powder releases six-times more alkalinity than the control soil. DETAILED DESCRIPTION \|[0015] It is to be understood that both the foregoing general description and the following detailed description are illustrative and explanatory, and are not restrictive of the subject matter, as claimed. In this application, the use of the singular includes the plural, the word “a” or “an” means “at least one”, and the use of “or” means “and/or”, unless specifically stated otherwise. Furthermore, the use of the term “including”, as well as other forms, such as “includes” and “included”, is not limiting. Also, terms such as “element” or “component” encompass both elements or components comprising one unit and elements or components that include more than one unit unless specifically stated otherwise. \|[0016] The section headings used herein are for organizational purposes and are not to be construed as limiting the subject matter described. All documents, or portions of documents, cited in this application, including, but not limited to, patents, patent applications, articles, books, and treatises, are hereby expressly incorporated herein by reference in their entirety for any purpose. In the event that one or more of the incorporated literature and similar materials defines a term in a manner that contradicts the definition of that term in this application, this application controls. \|[0017] Climate change fundamentally threatens the safety and stability of modern civilization. In order to avoid the increasingly disastrous and costly effects of climate change, net atmospheric concentrations of greenhouse gases must be reduced. Such reductions can be achieved through improvements in productive efficiency (e.g., reducing CO2 emissions while maintaining output) and carbon dioxide (CO2) removal (CDR).\|[0018] Enhanced rock weathering (ERW) is an example of a CDR-based approach that aims to take atmospheric Carbon (CO2) out of air and store it as bicarbonate or carbonate. ERW has been investigated in cropland but not in golf courses or other managed turfs. Several different types of materials have been used for ERW, including peridotite, basalt, slag, and mine-tailings. Furthermore, ERW has beneficial effects on soil health by releasing beneficial mineral nutrients into the soil, such as calcium, potassium, phosphorous, and magnesium. \|[0019] However, ERW-based CDR processes utilizing peridotites, mine tailings, slag, and basalt other than tholeiites have numerous limitations. Foremost among them is the potential release of heavy metals to the environment and slow weathering kinetics. Furthermore, manufacturing large amounts of basalt powder (including mining, crushing, sorting, and shipping) can be an energy intensive process. Moreover, there is additional energy required to apply the basalt powder multiple times throughout the growing season with specialized spreading equipment that is typically gas powered. These costs and methods to spread the products for ERW would be especially difficult in places where this spreading is not common practice. This results in increased development costs and increased energy consumption. Such limitations may render ERW-based CDR processes inefficient and impractical for large scale CO2 capture from large surface areas. \|[0020] In comparison, golf course greens and courses at large, which, in general, are intensively managed, already engage in this top sanding process. They own and have the technical expertise to spread large amounts of sand onto the turf surface and rootzone. There are large amounts of research into turf grass and golf course maintenance practices aiding the development and deployment of basalt sands within existing maintenance and construction. Additionally, Golf courses have many characteristics that make them ideal to engender CDR through ERW as they are frequently located in warm and hot climates, are frequently watered and receive precipitation, and have high levels of primary productivity leading to turfs generating large amounts of organic matter—three parameters that increase the weathering rate. \|[0021] In sum, current methods of capturing CO2 have numerous limitations in terms of efficacy, efficiency, costs, and the ability to capture CO2 from large surface areas. Numerous embodiments of the present disclosure address the aforementioned limitations. \|[0022] Basalt sand compositions\|[0023] In some embodiments, the present disclosure pertains to compositions that include at least one basalt sand. Basalt is the name of a mafic aphanitic volcanic rock that includes, without limitation, tholeiites. Basalt is exposed around the world on the continents and at the ocean floor. The basalt sands of the present disclosure may be in various forms. For instance, in some embodiments, the basalt sand is in isolated form (i.e., basalt sand isolated from its native environment). In some embodiments, the basalt sand is in the form of crushed particles. In some embodiments, the basalt sand is in purified form. In some embodiments, the basalt sand includes pre-treated basalt sand. In some embodiments, the basalt sands of the present disclosure may be in the form of course particles, medium particles, course-grained particles, fine-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. \|[0024] The basalt sands of the present disclosure may include various compounds. For instance, in some embodiments, the compounds may include, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4, or combinations thereof. \|[0025] The compositions of the present disclosure may include various types of basalt sands. In some embodiments the basalt sand includes a plurality of different types of basalt sands. In some embodiments, the basalt sand includes, without limitation, plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. \|[0026] In some embodiments, the basalt sand compositions of the present disclosure include plagioclase feldspars-containing basalts and pyroxenes-containing basalts. In some embodiments, the basalt sand compositions of the present disclosure include microscopic or visible plagioclase feldspars-containing basalts and pyroxenes-containing basalts, with little or no olivines, and with minor iron spinel and phosphate. \|[0027] In some embodiments, the basalt sand compositions of the present disclosure include tholeiites. In some embodiments, the basalt sand compositions of the present disclosure include tholeiites with low heavy metal concentrations.\|[0028] In some embodiments, the basalt sand compositions of the present disclosure include Holyoke Basalt. In some embodiments, the Holyoke Basalt is derived from Massachusetts (MA). In some embodiments, the average concentrations of Cr, Ni, Cu, Zn, and Pb in Holyoke Basalt are 13 ppm, 33 ppm, 78 ppm, 86 ppm, and 4 ppm, respectively. In some embodiments, the average concentrations of Cr, Ni, Cu, Zn, and Pb in Holyoke Basalt are 384 ppm, 75 ppm, 145 ppm, 88 ppm, and 1.5 ppm, respectively. In some embodiments, Holyoke Basalt is essentially devoid of visible crystals. In some embodiments, Holyoke Basalt is in non-crystalline form. In some embodiments, Holyoke Basalt includes the following elements: SiO2, TiO2, Al2O3, Fe2O3, FeO, CaO, MgO, MnO, K2O, Na2O, and P2O5. \|[0029] In some embodiments, the basalt sand compositions of the present disclosure include Butner Basalt. In some embodiments, the Butner Basalt is derived from North Carolina (NC). In some embodiments, Butner Basalt is essentially devoid of visible crystals. In some embodiments, Butner Basalt is in non-crystalline form. \|[0030] In some embodiments, Holyoke Basalt and Butner Basalt each include the following elements: SiO2, TiO2, Al2O3, Fe2O3, FeO, CaO, MgO, MnO, K2O, Na2O, and P2O5. In some embodiments, the aforementioned elements are present at average weight percentages listed in Table 1. Table 1. Average weight percentages of major elements of Holyoke and Butner Basalts. The data are averages of published results downloaded from GEOROC.org. () FeO for Butner basalt reflects the total amount of iron present without making a distinction between Fe(II) and Fe(III). (*) EPOT is the maximum enhanced weathering CO2 capture potential in units of kg CO2 t-1 (as defined in Renforth (2019) The negative emission potential of alkaline materials. Nature Comm. https://doi.org/10.1038/s41467-019-09475-5). \|[0031] The basalt sands of the present disclosure may include various particle shapes. For instance, in some embodiments, the basalt sand particles of the present disclosure may be angular or rounded depending on their application. In some embodiments, different proportions of basalt sand particle sizes and blends may be used to best suit the local conditions. For instance, in some embodiments, finer sands may retain more moisture within an upper rootzone of a soil. In some embodiments, such sands may also include reduced moisture content through various treatment methods (e.g., kiln drying) so that they can be applied to a surface more effectively (e.g., more efficient spreading using golf course sand spreading and aeration equipment). \|[0032] The compositions of the present disclosure may also include additional components. For instance, in some embodiments, the compositions of the present disclosure may also include one or more additives. In some embodiments, the one or more additives include, without limitation, silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz- based top sands, lime, or combinations thereof.\|[0033] In some embodiments, the additives include one or more golf course additives. In some embodiments, the golf course additives include, without limitation, peat moss, quartz-based top sands, lime, or combinations thereof. In some embodiments, the quartz-based top sands are utilized to dilute the basalt. In some embodiments, the basalt sand compositions of the present disclosure may be treated with such additives depending on the needs of a surface (e.g., a local soil). \|[0034] Methods of modifying a surface \|[0035] Additional embodiments of the present disclosure pertain to methods of modifying a surface. In some embodiments, such methods include applying a composition of the present disclosure to the surface. Suitable compositions were described supra and are incorporated herein by reference. \|[0036] The compositions of the present disclosure may be applied to surfaces in various manners. For instance, in some embodiments, the compositions of the present disclosure may be applied by methods that include, without limitation, spreading, pouring, sprinkling, spraying, or combinations thereof. In some embodiments, the compositions of the present disclosure are placed on an outer layer of the surface. In some embodiments, the compositions of the present disclosure may become integrated with the surface. In some embodiments, the methods of the present disclosure may also include a step of removing an outer layer of a surface prior to applying a composition of the present disclosure to the surface. \|[0037] FIGS. 1A-1C, 2A-2B, 3A-3C, and 4A-4C illustrate exemplary processes for applying a composition of the present disclosure to a surface. For instance, FIGS.1A-1C illustrate an exemplary process for applying a composition of the present disclosure (i.e., basalt sand 14) to a surface 10 with an outer layer 12. In this example, outer layer 12 is first removed from surface 10 (FIG. 1A). Thereafter, basalt sand 14 is applied to surface 10 (FIG.1B) to form a new outer layer 16 on surface 10, which contains basalt sand 14 (FIG.1C). \|[0038] FIGS.2A-2B show an example of a more specific process to integrate an existing surface (i.e., a top sand 30 of a golf course) with a composition of the present disclosure (i.e., basalt sand 34) to build up a new outer layer 36 where basalt sands 34 are integrated in the top sand 30 of the greens and turf surface generally. As illustrated in FIG.2A, basalt sand 34 is applied to top sand 30 of a golf course with an outer layer (i.e., the grass and rootzone 32). In some embodiments, basalt sand 34 may be applied with agricultural spreaders, such as equipment 35, to top sand 30. As illustrated in FIG. 2B, the application of basalt sands 34 forms a new outer layer 36 on surface 30, which contains composition 34 integrated into surface 30 (FIG.2B). \|[0039] FIGS. 3A-3C show another specific method of integrating the compositions of the present disclosure (i.e., basalt sand 44) into a surface (i.e., a top sand 40 with topsoil 42) by using aeration as a chance to rapidly integrate larger amounts of basalt sands 44 deeper into the root zone of top sand 40. In this Example, equipment 43 is used to punch holes 45 into surface 40 of the grass. In some embodiments, such as process may remove around 10% of the organic matter dense root zone and topsoil 42 (FIGS.3A-3B). Thereafter, the same spreading equipment 43 may be used to backfill holes 45 with basalt sands 44 (FIGS. 3B-3C). This process is not only beneficial for managing organic matter in the surface and overall grass health, but also will allow basalt sands to penetrate deeper into the surface of the green. \|[0040] FIGS. 4A-4C show another specific method to integrate the compositions of the present disclosure (i.e., basalt sands 54) into a surface (i.e., top sand 50 with an outer layer 52). In this example, outer layer 52 is first removed from surface 50 (FIG.4A). Thereafter, composition 54 is applied to surface 50 (FIG.4B) to form a new outer layer 56 on surface 50, which contains composition 54 (FIG. 4C). In some embodiments, this option allows for a large amount of basalt sand to be used as the entire soil profile will be entirely rebuilt and basalt sands can be included in the blend as well as in the sand spread into the rootzone as the grass is regrown.\|[0041] The compositions of the present disclosure may be applied to a surface at various concentrations. For instance, in some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 0.1 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 0.5 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 1 ton per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 2 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 2.5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 7.5 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 10 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 25 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 50 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 75 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 100 tons per acre of the surface. \|[0042] The compositions of the present disclosure may be applied to a surface at varying levels of frequency. For instance, in some embodiments, the compositions of the present disclosure may be applied to a surface from one time to twenty times per year. In some embodiments, the compositions of the present disclosure may be applied to a surface from one time to five times per year. \|[0043] In some embodiments, full aeration and backfilling holes of a surface may only be done one to five times per year. Since a larger volume of soil may be removed through aeration, more top sand may be needed during aeration than regular top sanding.\|[0044] The compositions of the present disclosure may be applied to various surfaces. For instance, in some embodiments, the surface is associated with a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. \|[0045] In some embodiments, the field includes managed turf. In some embodiments, the managed turf is in the form of a monoculture. In some embodiments, the managed turf may require constant attention and maintenance as well as a high amount of nutrients and agricultural additives to keep the turf growing consistently. \|[0046] In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course, such as, but not exclusive to the accredited golf courses outlined in FIG.5. \|[0047] In some embodiments, the surface includes a soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0048] In some embodiments, the methods of the present disclosure also improve the quality of the soil. For instance, in some embodiments, the improved soil quality includes at least one of nutrient enhancement, enhanced CO2 capture, enhanced soil fertility, enhanced soil health, optimization of soil pH, or combinations thereof. As an example, soils developed on Holyoke Basalt as well as Blue ridge basalts have higher pH than those developed on surrounding rocks. They are also richer in nutrients, especially exchangeable Ca and Mg than soil. Table 2 compares soil pH, Organic Matter (OM) and cations on soils developed on north and south sides of ridges made of Holyoke Basalt in Massachusetts. Here, the concentrations are in ppm and uncertainties given in parentheses. The soils developed on Holyoke Basalt have low concentrations of heavy metals. Table 2. A comparison of soil pH, Organic Matter (OM) and cations on soils developed on north and south sides of ridges made of Holyoke Basalt in Massachusetts (data is from Karen B. Searcy, Brayton F. Wilson and James H. Fownes, The Journal of the Torrey Botanical Society, 2003, 130 (3), pp.158-169). \|[0049] In some embodiments, the improved soil quality provides various advantages. For instance, in some embodiments, the improved soil quality reduces or eliminates a need for the use of one or more soil nutrients, one or more soil fertilizers, additives (e.g., lime), or combinations thereof. \|[0050] Modified Surfaces \|[0051] Additional embodiments of the present disclosure pertain to modified surfaces. In some embodiments, the modified surfaces of the present disclosure include a composition of the present disclosure. Suitable compositions were described supra and are incorporated herein by reference.\|[0052] The compositions of the present disclosure may be associated with surfaces in various manners. For instance, in some embodiments, the compositions of the present disclosure are positioned on an outer layer of the surface. FIG.1C illustrates an example of a modified surface 20. In this example, modified surface 20 includes surface 10 with an outer layer 16 that contains a composition of the present disclosure 14. FIG.2B illustrates another example of a modified surface 39. In this example, modified surface 39 includes a surface 30 with an outer layer 36. In this example, a composition of the present disclosure 34 is integrated into surface 30 and outer layer 36. FIG.3C illustrates another example of a modified surface 49. In this example, modified surface 49 includes a surface 40 that contains a composition of the present disclosure 44 integrated into the surface. FIG. 4C illustrates another example of a modified surface 60. In this example, modified surface 60 includes a surface 50 with outer layer 56 that contains a composition of the present disclosure 54 integrated into the surface. \|[0053] The modified surfaces of the present disclosure may include various concentrations of the compositions of the present disclosure. For instance, in some embodiments, the composition is at a concentration of at least about 0.1 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 0.5 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 1 ton per acre of the surface. In some embodiments, the composition is at a concentration of at least about 2 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 2.5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 7.5 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 10 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 25 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 50 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 75 tons per acre of the surface. In some embodiments, the composition is at a concentration of at least about 100 tons per acre of the surface.\|[0054] In some embodiments, the modified surfaces of the present disclosure are associated with a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course. \|[0055] In some embodiments, the modified surfaces of the present disclosure include a soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0056] In some embodiments, the composition improves the quality of the soil. For instance, in some embodiments, the improved soil quality includes at least one of nutrient enhancement, enhanced CO2 capture, enhanced soil fertility, enhanced soil health, optimization of soil pH, or combinations thereof. In some embodiments the improved soil quality reduces or eliminates a need for the use of one or more soil nutrients, one or more soil fertilizers, additives (e.g., lime), or combinations thereof. \|[0057] Methods of CO2 Capture from an Environment \|[0058] Additional embodiments of the present disclosure pertain to methods of capturing carbon dioxide (CO2) from an environment. In some embodiments, such methods include exposing the environment to a composition of the present disclosure. Suitable compositions were described supra and are incorporated herein by reference. In some embodiments, the basalt sands in the compositions of the present disclosure capture the CO2. \|[0059] The methods of the present disclosure may be utilized to capture CO2 from various environments. For instance, in some embodiments, the environment includes, without limitation, an airstream, a gas stream, an industrial plant, an atmosphere, ambient air, or combinations thereof. In some embodiments, the environment includes ambient air. \|[0060] Various methods may also be utilized to expose an environment to a composition of the present disclosure. For instance, in some embodiments, the exposing occurs by flowing the environment through the composition. In some embodiments, the exposing occurs by placing the composition at or near the environment.\|[0061] In some embodiments, the exposing occurs by applying the composition to a surface. Various methods may be utilized to apply the compositions of the present disclosure to a surface. For instance, in some embodiments, the application occurs by a method that includes, without limitation, spreading, pouring, sprinkling, spraying, or combinations thereof. \|[0062] In some embodiments, the methods of the present disclosure also include a step of removing an outer layer of a surface prior to applying the composition to the surface. In some embodiments, the composition is placed on an outer layer of the surface. \|[0063] The methods of the present disclosure may capture CO2 from various surfaces. For instance, in some embodiments the surface includes soil. In some embodiments, the soil includes, without limitation, top sand, topsoil, a turf, a managed turf, a soil layer below grass, or combinations thereof. In some embodiments, the surface includes a soil layer below grass. In some embodiments, the surface includes a soil layer below grass and its root zones. \|[0064] In some embodiments, the surface includes a field. In some embodiments, the field includes an agricultural field, a residential field, a golf course, a park, a sports facility, a yard, a highway, a subdivision, or combinations thereof. In some embodiments, the field includes a golf course. In some embodiments, the golf course includes a USGA accredited golf course. \|[0065] The compositions of the present disclosure may be applied to surfaces at various concentrations for CO2 capture. For instance, in some embodiments, the composition is applied at a concentration of at least about 0.1 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 0.5 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 1 ton per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 2 tons per acre of the surface per year. In some embodiments the composition is applied at a concentration of at least about 2.5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 7.5 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 10 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 25 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 50 tons per acre of the surface per year. In some embodiments, the composition is applied at a concentration of at least about 75 tons per acre of the surface per year. In some embodiments, the compositions of the present disclosure are applied at a concentration of at least about 100 tons per acre of the surface. \|[0066] The methods of the present disclosure may be utilized to capture various types of CO2. For instance, in some embodiments, the captured CO2 includes atmospheric CO2. In some embodiments, the captured CO2 includes CO2 embedded within a surface. \|[0067] Without being bound by theory, CO2 capture may occur by various mechanisms. For instance, in some embodiments, CO2 capture may occur by at least one of sequestration, direct capture, adhesion, binding, adsorption, electrostatic interaction, or combinations thereof. \|[0068] Without being bound by further theory, CO2 capture may occur through various chemical reactions. For instance, in some embodiments, the CO2 capture occurs by a reaction between at least one basalt sand, CO2, and water. In some embodiments, the reaction releases one or more alkaline ions and mineralized bicarbonate (HCO3-). In some embodiments, the reactions combine HCO3- with Ca2+ ions to produce stable CaCO3 mineral.\|[0069] Without being bound by further theory, CO2 capture can occur through various reactions of silicate minerals, CO2, and H2O. For instance, in some embodiments where the basalt sand includesa CO2 capture reaction can occur through the reaction shown in equation 1.\|[0070] In some embodiments where the basalt sand includes NaAlSi3O8, a CO2 capture reaction can occur through the reaction shown in equation 2.\|[0071] In some embodiments where the basalt sand includes (Ca, Mg)2Si2O6, a CO2 capture reaction can occur through the reaction shown in equation 3.\|[0072] In some embodiments where the basalt sand includes (Mg, Fe)2SiO4, a CO2 capture reaction can occur through the reaction shown in equation 4.\|[0073] In some embodiments, atmospheric CO2 removed by a CO2 capture reaction is either retained as a long lived HCO3- or a CaCO3 precipitate. In some embodiments, production of these compounds leads to net removal of atmospheric CO2\|[0074] In some embodiments, Ca2+ and HCO3- react in accordance with equation 5 to result in the precipitation of CaCO3\|[0075] Methods of making basalt sand compositions \|[0076] Additional embodiments of the present disclosure pertain to methods of making the basalt sand compositions of the present disclosure. In some embodiments, such methods include crushing at least one basalt sand such that the crushing results in the formation of crushed basalt sand particles.\|[0077] In some embodiments, the methods of the present disclosure also include a step of isolating, filtering and/or drying the basalt sand. In some embodiments, the methods of the present disclosure include a step of filtering basalt sand based on the particle size of the basalt sand. In some embodiments, the isolating occurs prior to the crushing. In some embodiments, the isolating includes purifying at least one basalt sand. \|[0078] The methods of the present disclosure may be utilized to crush various basalt sands. Suitable basal sands were described supra and are incorporated herein by reference. For instance, in some embodiments, the basalt sands include, without limitation, plagioclase feldspars-containing basalts, pyroxenes-containing basalts, tholeiites, Holyoke Basalts, Blue Ridge Basalts, Butner Basalts, or combinations thereof. In some embodiments, at least one basalt sand includes a compound that includes, without limitation, CaAl2Si2O8, (Ca, Mg)2Si2O6, (Mg, Fe)2SiO4, NaAlSi3O8, (Ca,Mg)SiO3, (Fe,Mg,Ca)2SiO4 or combinations thereof. \|[0079] Various methods may be utilized to crush basalt sands. For instance, in some embodiments, the crushing occurs by methods that include, without limitation, grinding, sonicating, pounding, compressing, milling (e.g., ball milling and/or hammer milling), or combinations thereof. In some embodiments, the crushed particles are in the form of fine-grained particles, course particles, medium particles, course-grained particles, ultra-fine particles, nanoparticles, microparticles, or combinations thereof. \|[0080] In some embodiments, the methods of the present disclosure also include a step of adding one or more additives to the basalt sand compositions. In some embodiments, the one or more additives include, without limitation, silicates, microbes, fungi, bacteria, actinomyces, biochar, golf course additives, peat moss, top sand, quartz-based top sands, lime, or combinations thereof. \|[0081] The methods of the present disclosure can have numerous embodiments. For instance, depending on the moisture content of the sands, kilns or other drying methods may be needed to produce spreadable top sand. \|[0082] Additional embodiments \|[0083] Reference will now be made to more specific embodiments of the present disclosure and experimental results that provide support for such embodiments. However, Applicants note that the disclosure below is for illustrative purposes only and is not intended to limit the scope of the claimed subject matter in any way.\|[0084] Example 1. Integrating Enhanced Rock Weathering (ERW) on Golf Courses \|[0085] This Example describes the deployment of enhanced rock weathering (ERW) practices alongside existing turf management programs to demonstrate the viability of ERW as a CO2 sequestration strategy for golf courses. This ERW strategy replaces traditional top sands with basalt sands for CO2 capture. \|[0086] Golf course construction typically entails a combination of subterranean drainage systems, irrigation, and the creation of an artificial topsoil consisting of a mixture of sand and soil to ensure proper drainage from the rootzone and base layer. In many cases, a “push-up green” is built with a custom blend of sand, peat moss (or other organic matter), and other additives. In some cases, a “sand- cap” is built over the existing sub-soil if the permeability is especially low. This is followed by layers of special soil, amended with sand to reduce the concentration of organic material (OM). An artificial topsoil may be necessary if the existing natural topsoil is too thin, lacking in nutrients, and/or over- compacted. Complete green construction guidelines are provided by the “USGA (2018). USGA Recommendations for a Method of Putting Green Construction.” \|[0087] After the topsoil has been created, seeding takes place and the “establishment period” begins. The grass begins to grow and root structures develop. \|[0088] Basalt sands could be integrated into existing golf course management programs. Moreover, when establishing a new course (or fully renovating an old course), designers can account for local conditions when integrating the basalt sands (e.g., climate, soil conditions, drainage, and/or local pests). \|[0089] Basalt sands could be used in laying the foundation for the entire course, incorporating many tons of crushed basalts into the sand-based root zone, and providing nutrient benefits to the surrounding soils and grasses. Additionally, fine-grained basalt sands could be used at multiple points in the development process with especially large quantities used during rootzone construction in addition to top sanding practices. Both cases provide an opportunity to integrate basalts effectively. \|[0090] The integration of basalt sands into the turf management programs at golf courses may bean optimal way to maximize the sequestration potential of golf courses. The highly managed soil structure of managed turf is ideally suited for enhanced rock weathering due to the high net primary productivity of the golf turf (estimated 1,100.5 g Carbon/m2/year), high volume of water flux from frequent irrigation, and existing systems for monitoring soil health, composition, and pH. (Wu, J., & Bauer, M. (2012). Estimating Net Primary Production of Turfgrass in an Urban-Suburban Landscape with QuickBird Imagery. Remote Sensing, Vol. 4, Issue 4, Pp. 849-866, 4, 849–866. https://doi.org/10.3390/rs4040849). \|[0091] This process has the potential to sequester an estimated 26 to 340 metric tons of carbon dioxide per golf course via green top and course wide sanding annually, depending on the integration level. With around 15,000 plus golf courses spread across the United States, this works out to an annual capture of between 391,000 and 5.15 million metric tons of CO2 per year from top dressing alone. \|[0092] These figures are calculated in Table 3. The sand application rates are derived from (Whitlark & Thompson, 2019; USGA Green Section Record, 57(9). https://www.usga.org/content/usga/home- page/course-care/green-section-record/57/9/light-and-frequent-topdressing-programs.html) and the sequestration rate of 20% is a rounded estimate based on current CDR potential figures from scientific literature, such as the basalts used in the Reershemius paper, which shows a capture potential of 183.56 kgCO2 t-1 (18.3%). This paper also discusses a potential method of measuring weathering based on a mass balance approach known as TiCAT. However, there are still questions regarding the effectiveness of this methodology (Reershemius, T., Kelland, M.E., Davis, I.R., D'Ascanio, R., Kalderon-Asael, B., Asael, D., Epihov, D.E., Beerling, D.J., Reinhard, C.T. and Planavsky, N.J., 2023. A new soil-based approach for empirical monitoring of enhanced rock weathering rates. arXiv preprint arXiv:2302.05004.). \|[0093] Additional simulations run on the MatLab weathering model from the Leverhulme Institute provided similar capture potential estimates of between 15-20% when parameters similar to that of a golf course soil profile were used. (Beerling et al., 2020, Nature, 583(7815), 242–248. https://doi.org/10.1038/s41586-020-2448-9; P. Renforth, 2012, International Journal of Greenhouse Gas Control, 10, 229–243). These estimates differ from the results in the lab experiment Applicants conducted using basalts from the Pioneer Valley.\|[0094] Regardless, in order to effectively measure and verify the amount of CO2 captured when basalt sands are deployed in the field, a reliable system of measurement must be developed. This verification process may include a variety of testing at individual courses. Various methods of measurement including, but not exclusive to, soil sampling, testing, other analyses, chemical testing, other laboratory or field-based testing, as well as sampling of water from existing drainage pipes and other sources around the course exist to conduct tests and analysis to verify weathering as well as the amount of CO2 sequestered. \|[0095] Tables 3-4 show the estimated values of carbon captured from golf courses. Calculations: Golf Course Annual Sand Use & CO2 Sequestration Potential EstimateCO2 Sequestration Tons/ Acre/ met. Tons/ hectare/ metric tons of Potential (metricTotal (Greens & Fairways – Combined)Table 3. Sand Use Estimates based on current industry top sand application rates and estimated CO2 Sequestration per golf course annual application. Table 4. Estimated range of value of Carbon Credits per golf course depending on the course integration level in USD($). \|[0096] The integration of basalt sands into the turf management practices of golf courses can be accomplished within existing infrastructure via putting green top sanding and aeration programs or through fairway top sanding. Although fairway top sanding and aeration is less common, recent golf turf grass studies emphasize the benefits of frequent and finer top sand applications to both greens and fairways. The adoption of course-wide top sanding significantly raises the sequestration opportunity to around 340 metric tons of CO2 per year. Depending on the course, basalt sands could also be used during construction or renovation to sequester greater amounts of CO2 once efficacy can be proven. \|[0097] To evaluate the extent to which alkalinity is released from basalt weathering, Applicants purchased rock powder Pioneer Valley basalt from Rock Dust Local (rockustlocal.com). This basalt is nearly identical in its chemical composition to that of Holyoke Basalt and has a maximum enhanced weathering CO2 capture potential of 203 kg CO2 t-1. The rock powder was dried and sieved. The particle size distribution of the rock power is shown in FIG.6.\|[0098] The basalt powder was mixed with sieved and dried soil from Dartmouth Organic Farm in a ratio of 10 g basalt to 170 g soil and packed in a Biorad® column to a height of ~6 cm. The soil used is Windsor loam. It is quite infertile and has not been fertilized. The column area is 23.76 cm2, meaning that the amount of basalt added is equivalent to 19 US ton/acre. As a control, 180 g of the same soil was also packed in columns as shown in FIG.7A. Water passed through the columns was weighed and measured for Na, K, Ca, and Mg. The alkalinity of the solution was also calculated. \|[0099] Experiments conducted over 3 months show that, with reference to the controls, the soil amended with basalt powder releases five-times more alkalinity (FIG. 7B). The data show that the basalt amended soil consumes 1.94 g of CO2 per 10 g of basalt (19.4% consumption) in comparison to soil control. This is equivalent to consumption of 194 kg of CO2 t-1 of basalt and approaches the theoretical maximum enhanced weathering CO2 capture potential for this rock. Additionally, the results are summarized in Table 5.Table 5. Changes in Alkalinity of effluent from basalt amended soil columns with reference to soil controls show that, on average, 19.4% of basalt was weathered over 88 days when 5 different elution experiments were conducted. Due to the time lag between experiments the total duration of experiments was about six months (May 2023-Oct 2023).\|[0100] While Applicants’ assessment of CO2 consumption per metric ton of basalt matches well with that recently reported experiment conducted over 4 years in an agricultural farm in Illinois (Beerling, D.J. et al. (2024) Enhanced weathering in the US Corn Belt delivers carbon removal with agronomic benefits, Proc. Nat. Acad. Sci.,121(9), e2319436121, https://doi.org/10.1073/pnas.2319436121), Applicants expect that the total CO2 consumed would be much higher in the golf courses, reaching the theoretical CO2 capture potential due to high temperatures and higher amounts of organic matter present in soil. \|[0101] Tables 6 and 7 provide general guidelines for top sands and USGA recommended root zones, respectively. Tables 6 and 7 provide recommended particle size distribution for a USGA approved Green rootzone construction, as well as a finer top sand blend that is based on the rootzone sand but with less coarse particles and more fine, ultra-fine, and other small particle sizes. A recent article (Whitlark & Thompson, 2019; USGA Green Section Record, 57(9). https://www.usga.org/content/usga/home-page/course-care/green-section-record/57/9/light-and- frequent-topdressing-programs.html) provided additional guidelines: “A general guideline is to select a sand that has a minimum of 50 percent of its particles in the medium-sized fraction (0.25-0.50 millimeters (mm) in diameter) and 15 to 40 percent in the coarse fraction (0.5-1.0 mm in diameter). The fine sand fraction (0.15-0.25 mm) should not exceed 25 percent, and the very fine fraction (0.05 – 0.15 mm) should not exceed 5 percent. Ideally, the material should have no particles greater than 1.0 mm in diameter given the difficulty in getting these larger particles to work down into the turf canopy. It is recommended to use a material with a coefficient of uniformity (CU) greater than 1.8. If the sand is too narrowly graded, which will produce a low CU, this may result in soft, unstable surfaces. However, the CU is not the only determining factor in stability – sand shape also plays a role, with angular sands being more stable. Utilizing a coarser sand during aeration will create more stability.” \|Typical Top sand GuidelinesTable 6. General guidelines for top sands.Table 7. General guidelines for USGA recommended root zones.\|[0102] Without further elaboration, it is believed that one skilled in the art can, using the description herein, utilize the present disclosure to its fullest extent. The embodiments described herein are to be construed as illustrative and not as constraining the remainder of the disclosure in any way whatsoever. While the embodiments have been shown and described, many variations and modifications thereof can be made by one skilled in the art without departing from the spirit and teachings of the invention. Accordingly, the scope of protection is not limited by the description set out above, but is only limited by the claims, including all equivalents of the subject matter of the claims. The disclosures of all patents, patent applications and publications cited herein are hereby incorporated herein by reference, to the extent that they provide procedural or other details consistent with and supplementary to those set forth herein.	Family Number\|(111402698)\|111402698\|Abstract\|(WO2024186724 A1)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.\|(AU2024233973 A1)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.(From WO2024186724 A1)\|(KR20250164234 A)\|Embodiments of the present disclosure are directed to compositions comprising at least one basalt sand in the form of crushed particles. A further embodiment of the present disclosure is directed to a method of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure are directed to modified surfaces comprising compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from the environment by exposing the environment to the compositions of the present disclosure, and methods of making basalt sand compositions of the present disclosure.\|(EP4676898 A1)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.\|(JP2026510743 A)\| The present invention relates to a composition containing at least one type of basalt sand in the form of crushed particles. A further embodiment of the disclosure relates to a method for modifying a surface by a step of applying the composition to the surface. Further embodiments of the disclosure relate to a modified surface containing the composition of the disclosure, a method for capturing carbon dioxide (CO2) from the environment by a step of bringing the environment into contact with the composition of the disclosure, and a method for preparing the basalt sand composition of the disclosure. Selected View Figure 2\|Title\|(WO2024186724 A1)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide\|(AU2024233973 A1)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide\|(KR20250164234 A)\|Integration of strengthening rock weathering and lawn management to isolate carbon dioxide in the atmosphere\|(CA3288102 A1)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide\|(EP4676898 A1)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide\|(JP2026510743 A)\|Integration of rock weathering acceleration and turf management to sequester atmospheric carbon dioxide\|Independent Claims\|(WO2024186724 A1)\|1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt (...) \|(AU2024233973 A1)\|1. A method of capturing carbon dioxide (CO2) from an environment, said method comprising: exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt sand captures (...) \|(KR20250164234 A)\|1. A method of capturing carbon dioxide (CO2) from an environment, the method comprising exposing the environment to a composition, wherein the composition comprises at least one basalt sand in the form of crushed particles, and wherein the at least one basalt (...) \|(JP2026510743 A)\|1. A method for capturing carbon dioxide (CO2) from the environment, which comprises a step of bringing the environment into contact with a composition, wherein the composition is The method comprises at least one kind of pulverized Basalt sand, and CO2 (...) \|	Chemical engineering\|Environmental technology\|Materials, metallurgy\|Other special machines	A01G-020/20\|B01D-053/62\|B01D-2257/504\|C04B-014/14\|C04B-022/10\|C04B-030/00\|C04B-2111/00019\|Y02C-020/40	(GR1) C04B-030/00[RK1]; C04B-014/14[RK2]; C04B-022/10[RK3]	A01G-020/20\|B01D-053/62\|B01D-2257/504\|C04B-014/14\|C04B-022/10\|C04B-030/00\|C04B-2111/00019\|Y02C-020/40	A01G-009/033\|A01G-020/00\|A01G-020/10\|A01G-020/20\|B01D-053/14\|B01D-053/62\|B01J-020/10\|C01B-033/24\|C01B-033/26\|C04B-014/04\|C04B-014/14\|C04B-022/10\|C04B-028/26\|C04B-030/00\|C04B-035/20\|C04B-111/00	A01G-009/033\|A01G-020/00\|A01G-020/10\|A01G-020/20\|B01D-053/14\|B01D-053/62\|B01J-020/10\|C01B-033/24\|C01B-033/26\|C04B-014/04\|C04B-014/14\|C04B-022/10\|C04B-028/26\|C04B-030/00\|C04B-035/20\|C04B-111/00					WO2022200450\|EP-826298	WO2022200450 101953667 WHO=Examiner SELF=N CAT=X CAT=Y\|EP-826298 573750 WHO=Examiner SELF=N CAT=X CAT=Y		WO2022200450; XP037187522; EP-826298; XP093211151\|\|\|\|\|	\|(WO2024/186724)\|International Search Report [Examiner]\|-BEERLING DAVID J.; KANTZAS EURIPIDES P.; LOMAS MARK R.; WADE PETER; EUFRASIO RAFAEL M.; RENFORTH PHIL; SARKAR BINOY; ANDREWS M. GR: "Potential for large-scale COremoval via enhanced rock weathering with croplands", NATURE, vol. 583, no. 7815, 8 July 2020 (2020-07-08), pages 242 - 248, XP037187522, DOI: 10.1038/s41586-020-2448-9\|-CHANG CHUNG CHIN: "A GRAVITY STUDY OF THE TRIASSIC VALLEY IN SOUTHERN CONNECTICUT", ECONOMIC AND ENVIRONMENTAL GEOLOGY, vol. 2, no. 2, 30 June 1969 (1969-06-30), XP093211151, ISSN: 1225-7281\|\|\|\|\|	PENDING	(EP4676898)\|PENDING\|(WO2024/186724)\|PENDING\|(JP2026510743)\|PENDING\|(KR10-2025-0164234)\|PENDING\|(AU2024233973)\|PENDING\|(CA3288102)\|PENDING	ALIVE	(EP4676898)\|ALIVE\|(WO2024/186724)\|ALIVE\|(JP2026510743)\|ALIVE\|(KR10-2025-0164234)\|ALIVE\|(AU2024233973)\|ALIVE\|(CA3288102)\|ALIVE	(EP4676898)\|LEGAL DETAILS FOR EP4676898\|Actual or expected expiration date=2044-03-04\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-04\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP 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PUBLISHED\|St27 status event code: A-1-1-Q10-Q12-NAP-PG1501 (AS PROVIDED BY THE NATIONAL OFFICE)\|(AU2024233973)\|LEGAL DETAILS FOR AU2024233973\|Actual or expected expiration date=2044-03-04\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-04\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2024233973\|Application date=2024-03-04\|Standardized application number=2024AU-0233973\|Event publication date=2025-10-23\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2024233973\|Publication stage code=A1\|Publication date=2025-10-23\|Standardized publication number=AU2024233973\|(CA3288102)\|LEGAL DETAILS FOR CA3288102\|Actual or expected expiration date=2044-03-04\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-04\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA3288102\|Application date=2024-03-04\|Standardized application number=2024CA-3288102\|Event publication date=2024-09-12\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA3288102\|Publication stage code=A1\|Publication date=2024-09-12\|Standardized publication number=CA3288102	(EP4676898)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4676898)\|Extension States: BA\|(EP4676898)\|Validation States: MA, MD, TN, KH, GE\|(WO2024/186724)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2024/186724)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2024/186724)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2024/186724)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2024/186724)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP4676898)\|EP\|(WO2024/186724)\|WO; AU; CA; EP; JP; KR\|(JP2026510743)\|JP\|(KR10-2025-0164234)\|KR\|(AU2024233973)\|AU\|(CA3288102)\|CA	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=iCBy9VOVqJVSDVsa5jTXaqCa4vFyxJplNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006578671&ekey=2380&xpn=EP4676898&kind=A1	https://register.epo.org/application?number=EP24767679	https://permalink.orbit.com/RenderStaticFirstPage?XPN=NfY8daI1uDcbWDK85JFymXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2024/186724)\|US	(WO2024/186724)\|NAME=TRUSTEES OF DARTMOUTH COLLEGE 11 Rope Ferry Road, #6210 Hanover, NH 03755-1404 , COUNTRY=US	(EP4676898)\|DE\|(WO2024/186724)\|US\|\|\|(AU2024233973)\|AU\|(CA3288102)\|CA	(EP4676898)\|NAME=Maiwald GmbH;Engineering Elisenhof Elisenstrasse 3 , CITY=80335 München , COUNTRY=DE , REG=101782373\|(WO2024/186724)\|NAME=AMINI, Farhang Shackelford, Bowen, McKinley & Norton, LLP 717 Texas Avenue, Suite 2700 Houston, TX 77002 , POSTCODE=77002 , COUNTRY=US\|(JP2026510743)\|NAME=YAMAMOTO Osamu , REG=100118902NAME=MIYAMAE,Toru , REG=100106208NAME=MATSUO JUNICHI , REG=100196508NAME=NAKAMURA MITSUTOSHI , REG=100126985\|(KR10-2025-0164234)\|NAME=KIM, JIN HOI NAME=KIM, TAE HONG\|(AU2024233973)\|NAME=PHILLIPS ORMONDE FITZPATRICK PO Box 24171 , CITY=Melbourne , STATE=VIC , POSTCODE=3001 , COUNTRY=AU\|(CA3288102)\|NAME=MBM INTELLECTUAL PROPERTY AGENCY 275 SLATER STREET, 14TH FLOOR , CITY=OTTAWA , POSTCODE=K1P 5H9 , COUNTRY=CA , REG=e61a1630-b292-4706-b91c-f3098c8c5df7	(EP4676898)\|US; US\|(WO2024/186724)\|US; US\|\|\|\|(CA3288102)\|US; US	(EP4676898)\|NAME=SHARMA, Mukul, CITY=Hanover, NH 03755-1404, COUNTRY=US \|NAME=MORRISON, Brian, CITY=Miami, FL 33156, COUNTRY=US\|(WO2024/186724)\|NAME=SHARMA, Mukul c/o Trustees of Dartmouth College 11 Rope Ferry Road, #6210 Hanover, NH 03755-1404, POSTCODE=03755-1404, COUNTRY=US \|NAME=MORRISON, Brian 7245 S.W. 125th Street Miami, FL 33156, POSTCODE=33156, COUNTRY=US\|(JP2026510743)\|NAME=Sharma, Mukuru\|(KR10-2025-0164234)\|NAME=MORRISON BRIAN\|NAME=SHARMA MUKUL\|(AU2024233973)\|NAME=MORRISON, Brian\|NAME=SHARMA, Mukul\|(CA3288102)\|NAME=MORRISON Brian 7245 S.W. 125th Street, CITY=Miami, POSTCODE=33156, STATE=FL , COUNTRY=US \|NAME=SHARMA Mukul c/o Trustees of Dartmouth College 11 Rope Ferry Road, #6210, CITY=Hanover, POSTCODE=03755-1404, STATE=NH , COUNTRY=US	(WO2024/186724)\|7\|(JP2026510743)\|7\|(KR10-2025-0164234)\|7\|(AU2024233973)\|7	2	6			(EP4676898)\|WO2024/186724\|(JP2026510743)\|WO2024/186724\|(KR10-2025-0164234)\|WO2024/186724\|(AU2024233973)\|WO2024/186724\|(CA3288102)\|WO2024/186724		(WO2024/186724)\|Number of Claims: NCL=54\|Extended kind: EXTK=x\|\|(JP2026510743)\|Number of Claims: NCL=54\|Request for examination: REQEXA=false\|\|(KR10-2025-0164234)\|Number of Claims: NCL=54\|\|(AU2024233973)\|Number of Claims: NCL=54\|		(EP4676898)\|ENGLISH (ENG)	(JP2026510743)\|Patent\|(EP4676898)\|Patent\|(KR20250164234)\|Patent\|(AU2024233973)\|Patent\|(CA3288102)\|Patent\|(WO2024186724)\|Patent	Titre: (EP4676898)\|Integrating enhanced rock weathering and turf management to sequester atmospheric carbon dioxide Résumé: (EP4676898)\|Embodiments of the present disclosure pertain to compositions that include at least one basalt sand that is in the form of crushed particles. Additional embodiments of the present disclosure pertain to methods of modifying a surface by applying a composition of the present disclosure to the surface. Further embodiments of the present disclosure pertain to modified surfaces that include the compositions of the present disclosure, methods of capturing carbon dioxide (CO2) from an environment by exposing the environment to a composition of the present disclosure, and methods of making the basalt sand compositions of the present disclosure.	14	Abstract	gpt-4o-mini	yes	The article discusses methods for capturing CO₂ using basalt sand, which is a silicate mineral, and focuses on enhanced rock weathering for carbon sequestration.
18	US63/638,100P\|US19/186,905	WOCA2025/050589\|US19/186,905	US20250333914\|WO2025/222295	116414688	WO2025/222295 A1 2025-10-30 [WO2025222295]\|US20250333914 A1 2025-10-30 [US20250333914]	2024-04-24\|2025-04-23	2025-04-23\|2025-04-23	2025-10-30\|2025-10-30		(US20250333914)\|2045-04-23\|(WO2025/222295)\|2027-10-24	(US20250333914)\|Carbon capture system and method for synthetic turf fields	(US20250333914)\|A synthetic turf system including a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes rock dust, or the synthetic turf system further includes a layer of the rock dust disposed above or below the one or more infill layers. The rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.	TARKETT SPORTS	(US20250333914)\|Tarkett Sports Canada Inc. ([CA])\|(WO2025/222295)\|TARKETT SPORTS CANADA INC. ([CA])	SMOLLETT JASON\|HABIB ERIC\|CHISAM CHRISTOPHER	(US20250333914)\|Smollett Jason\|Habib Eric\|Chisam Christopher	(WO2025/222295)\|YIP, Vincent ([CA])	(US20250333914)\|Furthermore, it will be appreciated that by placing the rock dust 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air.\|It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the rock dust 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-7 are intended solely as one non-limiting example of turf carpet systems in which the rock dust 102 may be utilized.\|	(US20250333914)\|1. A synthetic turf system comprising: a backing; turf fibers extended upward from the backing; and one or more infill layers positioned above the backing, below a top portion of the turf fibers, wherein the one or more infill layers includes rock dust, or the synthetic turf system further comprises a layer of the rock dust disposed above or below the one or more infill layers, and the rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.\|14. Infill for a synthetic turf system, the infill comprising: rock dust including silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, wherein at least 90 percent of the rock dust has a particle size less than 250 micrometers in diameter; and organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust in one or more infill layers.\|17. A method of preparing a synthetic turf system, the method comprising: dispersing rock dust over a top portion of turf fibers, wherein the rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|	(US20250333914)\|As used in this application, "or" is intended to mean an inclusive "or" rather than an exclusive "or".\|In accordance with some aspects described herein, there is provided an synthetic turf system that utilizes a material derived from one or more types of rock dust, including, for example and without limitation, basalt rock dust, igneous rock dust (such as andesite, diorite, gabbro, or rhyolite), limestone-derived dust (such as calcium carbonate-based materials), dolomitic lime (CaO/MgO), ultramafic rock dust (such as peridotite or dunite), industrial byproducts containing reactive silicates or carbonates, a blend of various types of rock dust, combinations thereof, or other similar mineral-based particulate materials.\|In yet another aspect, a layer of rock dust-based particles may be positioned on a geotextile or subgrade layer.\|	(US20250333914)\|ROCK DUST(100,77)\|SYNTHETIC TURF FIELD(100,3)\|CARBON CAPTURE(100,2)\|TURF FIBER(73,32)\|INFILL LAYER(72,54)\|SILICATE ROCK(66,14)\|ROCK REACTION(58,13)\|SYNTHETIC TURF(54,62)\|ROCK DUST INCORPORATION(52,1)\|ROCK DUST PLACEMENT(46,1)\|RAINWATER(42,29)\|BACKING(39,28)\|LIMESTONE DERIVED DUST(39,1)\|IGNEOUS ROCK(38,11)\|ULTRAMAFIC ROCK DUST(38,1)\|BASE ROCK LAYER(37,46)\|IGNEOUS ROCK DUST(36,1)\|ELASTOMER PARTICLE(34,5)\|THERMOPLASTIC PARTICLE(33,5)\|DISPERSING ROCK(33,2)\|SILICATE REACTION(33,1)\|ROCK DUST PARTICLE(32,3)\|LAYERED INSTALLATION(32,1)\|ROCK DUST PARTICLE LAYER(32,1)\|BICARBONATE(31,11)\|DUST(30,9)\|ROCK(27,53)\|DOLOMITIC LIME(27,4)\|RUBBER PARTICLE(26,5)\|PERIDOTITE(26,4)\|ANDESITE(25,4)\|RHYOLITE(25,4)\|BYPRODUCT(25,1)\|DIORITE(24,4)\|AMERICAN SOCIETY(24,1)\|SUBGRADE LAYER(24,1)\|SYNTHETIC TURF BACKING(24,1)\|COATED PARTICLE(23,5)\|DUNITE(23,4)\|ANDTHE(23,2)\|GEOTEXTILE(23,1)\|SYNTHETIC TURF INFILL LAYER(23,1)\|BASALT(22,5)\|ORGANIC PARTICLE(22,5)\|WEATHERED PARTICLE(22,2)\|ANDONE(22,1)\|TURF(22,1)\|INFILL(21,6)\|DUST PARTICLE(21,5)\|GEOTEXTILE COMPONENT(20,10)\|SUBGRADE(18,10)\|WOLLASTONITE(18,4)\|QUICKLIME(18,3)\|INCH EIGHTH(17,2)\|MINERAL PARTICULATE MATERIAL(17,1)\|BLEND(15,1)\|SPHERICITY(13,3)\|CALCIUM CARBONATE MATERIAL(13,1)\|INFILL LAYER THICKNESS(12,2)\|ORTHE(12,1)\|ASTM(11,4)\|CARBONATE MATERIAL(11,1)\|GROUND(10,3)\|SHOCK PAD(8,6)\|BICARBONATE SUBSTANCE(8,4)\|TOP DRESSING(8,3)\|PARTICLE SIZE(7,7)\|CARBONATE SEDIMENT(7,2)\|WENTWORTH AGGREGATE CLASSIFICATION(7,1)\|DRAINAGE PIPE(6,2)\|ROCK DUST REACTION(6,2)\|AERIAL SPREADER(6,1)\|ARTIFICIAL TURF INFILL(6,1)\|BALLAST INFILL(6,1)\|COMPACTION VARIABILITY(6,1)\|CONJOINED CLAUSE(6,1)\|ENGINEERED DRAINAGE(6,1)\|HANDHELD SPREADER(6,1)\|LAYMOR BRUSH(6,1)\|MESH SIZE(6,1)\|PERMEABLE SUBGRADE(6,1)\|PROPYLENE DIENE MONOMER(6,1)\|TURF BRUSHING EQUIPMENT(6,1)\|CARBON DIOXIDE(5,10)\|BROADCASTER TOOL(5,1)\|ENDPOINT RECITATION(5,1)\|IMPERMEABLE BARRIER(5,1)\|OSCILLATING BRUSH(5,1)\|PARTICLE SIZING(5,1)\|PERMEABLE BACKING(5,1)\|PNEUMATIC SPREADER(5,1)\|ROCK COMPACTION(5,1)\|ROCK DUST MIXING(5,1)\|SANDY SOILS(5,1)\|SEED TENDER(5,1)\|STONE DISPERSION(5,1)\|STORM DRAIN OUTLET(5,1)\|WALK BEHIND ROTARY BRUSH(5,1)\|CARBONIC ACID(4,7)\|INFILL MATERIAL(4,6)\|CARPET(4,3)\|STORM WATER(4,3)\|ULTRAMAFIC ROCK(4,3)\|DEACIDIFYING(4,2)\|HOPPER GATE(4,2)\|AIR BOOM SPREADER(4,1)\|BALL INTERACTION(4,1)\|DRAINAGE ELEVATION(4,1)\|GEOTEXTILE FABRIC LAYER(4,1)\|HYDRAULIC BRUSH(4,1)\|NATURAL BYPRODUCT(4,1)\|RAINWATER POOLING FLOW(4,1)\|ROCK BLEND(4,1)\|SUBDRAIN TRENCH BOTTOM(4,1)\|SYNTHETIC TURF INSTALLATION(4,1)\|TRIANGULAR BRUSH(4,1)\|ROCK DUST LAYER(3,9)\|NOMINAL SIZE RANGE(3,4)\|RIVER(3,4)\|SEA(3,4)\|DOLOMITE(3,2)\|HYDRAULICALLY CONTROLLED CONVEYER(3,2)\|MINERAL NUTRIENT(3,2)\|OLIVINE(3,2)\|THERMOPLASTIC(3,2)\|TRACTION(3,2)\|COMPACTED STONE BASE(3,1)\|DESCRIPTOR(3,1)\|FLEXIBLE BRUSH(3,1)\|INFILL LAYER LAYERED ARRANGEMENT(3,1)\|MODIFIED SUBGRADE(3,1)\|PACKING STABILITY(3,1)\|PARTICLE ETHYLENE(3,1)\|RAIN WATER REACTION(3,1)\|RIGID BRUSH(3,1)\|ROCK DUST COMPOSITIONAL RANGE(3,1)\|ROTARY BRUSH ACTION(3,1)\|STRAIGHT BRUSH(3,1)\|\|(WO2025/222295)\|ROCK DUST(100,80)\|SYNTHETIC TURF FIELD(100,4)\|CARBON CAPTURE(100,3)\|TURF FIBER(77,32)\|INFILL LAYER(74,54)\|SILICATE ROCK(65,14)\|ROCK REACTION(57,13)\|SUBDRAIN TRENCH(54,5)\|SYNTHETIC TURF(53,62)\|ROCK DUST INCORPORATION(51,1)\|BACKING(47,28)\|ROCK DUST PLACEMENT(45,1)\|RAINWATER(41,29)\|GEOTEXTILE FABRIC(40,1)\|IGNEOUS ROCK(38,11)\|BASE ROCK LAYER(37,46)\|GEOTEXTILE FABRIC LAYER(34,1)\|ELASTOMER PARTICLE(33,5)\|DISPERSING ROCK(33,2)\|THERMOPLASTIC PARTICLE(32,5)\|ROCK DUST PARTICLE(32,3)\|LAYERED INSTALLATION(31,1)\|ROCK DUST PARTICLE LAYER(31,1)\|BICARBONATE(30,11)\|SUBDRAIN TRENCH BOTTOM(30,1)\|INFILL(27,7)\|RUBBER PARTICLE(25,5)\|ROCK(24,53)\|AMERICAN SOCIETY(23,1)\|GEOTEXTILE(23,1)\|SUBGRADE LAYER(23,1)\|SYNTHETIC TURF BACKING(23,1)\|SYNTHETIC TURF INFILL LAYER(23,1)\|COATED PARTICLE(22,5)\|ORGANIC PARTICLE(22,5)\|WEATHERED PARTICLE(22,2)\|ENVIRONMENTALLY FRIENDLY(22,1)\|TURF(22,1)\|DUST PARTICLE(21,5)\|TRANSPORTATION(21,1)\|GEOTEXTILE COMPONENT(20,10)\|DUST(18,6)\|QUICKLIME(18,3)\|DOLOMITIC LIME(17,4)\|PERIDOTITE(17,4)\|WOLLASTONITE(17,4)\|ANDESITE(16,4)\|DIORITE(16,4)\|RHYOLITE(16,4)\|INCH EIGHTH(16,2)\|ROCK DUST MATERIAL(16,1)\|DUNITE(15,4)\|BASALT(14,5)\|SPHERICITY(12,3)\|INFILL LAYER THICKNESS(12,2)\|ASTM(11,4)\|CARBON NEUTRAL(11,1)\|DUST MATERIAL(11,1)\|SHOCK PAD(8,6)\|BICARBONATE SUBSTANCE(8,4)\|CARBON OFFSETTING MATERIAL(8,1)\|PARTICLE SIZE(7,7)\|TOP DRESSING(7,3)\|CARBONATE SEDIMENT(7,2)\|MECHANICAL RESISTANCE(7,1)\|WENTWORTH AGGREGATE CLASSIFICATION(7,1)\|MECHANICAL PROPERTY(6,3)\|DRAINAGE PIPE(6,2)\|ROCK DUST REACTION(6,2)\|CONJOINED CLAUSE(6,1)\|AERIAL SPREADER(5,1)\|ARTIFICIAL TURF INFILL(5,1)\|BALLAST INFILL(5,1)\|BROADCASTER TOOL(5,1)\|COMPACTION VARIABILITY(5,1)\|ENDPOINT RECITATION(5,1)\|ENGINEERED DRAINAGE(5,1)\|HANDHELD SPREADER(5,1)\|IMPERMEABLE BARRIER(5,1)\|LAYMOR BRUSH(5,1)\|LIMESTONE DERIVED DUST(5,1)\|MESH SIZE(5,1)\|OSCILLATING BRUSH(5,1)\|PARTICLE SIZING(5,1)\|PERMEABLE BACKING(5,1)\|PERMEABLE SUBGRADE(5,1)\|PNEUMATIC SPREADER(5,1)\|PROPYLENE DIENE MONOMER(5,1)\|ROCK COMPACTION(5,1)\|ROCK DUST MIXING(5,1)\|SANDY SOILS(5,1)\|SEED TENDER(5,1)\|STONE DISPERSION(5,1)\|STORM DRAIN OUTLET(5,1)\|TURF BRUSHING EQUIPMENT(5,1)\|ULTRAMAFIC ROCK DUST(5,1)\|WALK BEHIND ROTARY BRUSH(5,1)\|CARBONIC ACID(4,7)\|INFILL MATERIAL(4,6)\|STORM WATER(4,3)\|DEACIDIFYING(4,2)\|HOPPER GATE(4,2)\|AIR BOOM SPREADER(4,1)\|BALL INTERACTION(4,1)\|DRAINAGE ELEVATION(4,1)\|HIGH AVAILABILITY(4,1)\|HYDRAULIC BRUSH(4,1)\|IGNEOUS ROCK DUST(4,1)\|NATURAL BYPRODUCT(4,1)\|RAINWATER POOLING FLOW(4,1)\|ROCK BLEND(4,1)\|SILICATE REACTION(4,1)\|SYNTHETIC TURF INSTALLATION(4,1)\|TRIANGULAR BRUSH(4,1)\|ROCK DUST LAYER(3,9)\|NOMINAL SIZE RANGE(3,4)\|RIVER(3,4)\|SEA(3,4)\|CARPET(3,3)\|DOLOMITE(3,2)\|HYDRAULICALLY CONTROLLED CONVEYER(3,2)\|MINERAL NUTRIENT(3,2)\|OLIVINE(3,2)\|THERMOPLASTIC(3,2)\|TRACTION(3,2)\|COMPACTED STONE BASE(3,1)\|DESCRIPTOR(3,1)\|FLEXIBLE BRUSH(3,1)\|INFILL LAYER LAYERED ARRANGEMENT(3,1)\|MODIFIED SUBGRADE(3,1)\|PACKING STABILITY(3,1)\|PARTICLE ETHYLENE(3,1)\|RAIN WATER REACTION(3,1)\|RIGID BRUSH(3,1)\|ROCK DUST COMPOSITIONAL RANGE(3,1)\|ROTARY BRUSH ACTION(3,1)\|STRAIGHT BRUSH(3,1)\|SYNTHETIC TURF MANUFACTURING(3,1)\|	(US20250333914)\|1. A synthetic turf system comprising:\| a backing;\| turf fibers extended upward from the backing; and\| one or more infill layers positioned above the backing, below a top portion of the turf fibers, wherein the one or more infill layers includes rock dust, or the synthetic turf system further comprises a layer of the rock dust disposed above or below the one or more infill layers, and\| the rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.\|2. The synthetic turf system of claim 1, wherein the rock dust includes wollastonite, basalt, peridotite, dunite, dolomitic lime, dolostone, andesite, diorite, gabbro, rhyolite, quick lime, or lime stone.\|3. The synthetic turf system of claim 1, wherein the rock dust includes silicate rock, igneous rock, or reactive rock.\|4. The synthetic turf system of claim 3, wherein the silicate rock, igneous rock, or reactive rock forms weathered particles having a sphericity of about 0.65 to about 0.85.\|5. The synthetic turf system of claim 1, further comprising a base stone layer disposed below the backing, and the rock dust is layered above, layered below, or mixed in the base stone layer.\|6. The synthetic turf system of claim 5, wherein the base stone layer is a first base stone layer formed from stone having a first nominal size range,\| the system further comprises a second base stone layer disposed below the first base stone layer, the second base stone layer having a second nominal size range coarser than the first nominal size range, and\| the rock dust is layered above, layered below, or mixed in the second base stone layer.\|7. The synthetic turf system of claim 6, wherein the first base stone layer is at least one inch thick and formed from American Society for Testing and Materials (ASTM) #89 stone, and the second base stone layer is at least 2 inches thick and formed from ASTM #57 stone.\|8. The synthetic turf system of claim 5, wherein the backing and the base stone layer are water permeable, and the rock dust is accessible by rainwater traveling through the one or more infill layers by gravity.\|9. The synthetic turf system of claim 5, wherein the base stone layer includes silicate rock, igneous rock, or reactive rock that is accessible to rainwater traveling from the top portion of the turf fibers by gravity.\|10. The synthetic turf system of claim 5, wherein the rock dust is layered directly on a top surface of the base stone layer, the rock dust forming a layer with a thickness of at least one eighth of an inch, or\| the rock dust is layered below a geotextile component, the rock dust forming a layer with a thickness of at least half an inch, the geotextile component being disposed underneath the base stone layer,\| the rock dust is tilled into a subgrade below the base stone layer, or\| the rock dust is positioned in a subdrain below the base stone layer.\|11. The synthetic turf system of claim 1, further comprising a subdrain trench below the backing, wherein the rock dust is blended with stone in the subdrain trench.\|12. The synthetic turf system of claim 1, wherein at least ninety percent of the rock dust has a particle size less than 62 micrometers in diameter.\|13. The synthetic turf system of claim 1, wherein the one or more infill layers include the rock dust, the one or more infill layers are disposed on top of the backing, between the turf fibers, and the top portion of the turf fibers extends above the one or more infill layers.\|14. Infill for a synthetic turf system, the infill comprising:\| rock dust including silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, wherein at least 90 percent of the rock dust has a particle size less than 250 micrometers in diameter; and\| organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust in one or more infill layers.\|15. The infill of claim 14, wherein the rock dust forms less than 10 percent of the infill by weight and includes wollastonite, basalt, peridotite, dunite, dolomitic lime, dolostone, andesite, diorite, gabbro, rhyolite, quick lime, or lime stone.\|16. The infill of claim 14, wherein 90 percent of the rock dust by weight has a particle size of 4 to 125 micrometers in diameter.\|17. A method of preparing a synthetic turf system, the method comprising:\| dispersing rock dust over a top portion of turf fibers, wherein the rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|18. The method of claim 17, further comprising:\| grooming the rock dust into the one or more infill layers of the synthetic turf system, between the turf fibers, at a backing of the synthetic turf system.\|19. The method of claim 17, further comprising:\| preblending the silicate rock, igneous rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the rock dust over the top portion of the turf fibers.\|20. The method of claim 17, further comprising:\| measuring an aspect of the synthetic turf system, including a thickness of an infill layer, an acidity of rainwater at the infill layer, or a quantity of silicate rock, igneous rock, or reactive rock present in the infill layer; and\| dispersing a predetermined quantity of the rock dust over the top portion of the turf fibers as a top dressing based on the measured aspect.	(US20250333914)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] The application claims priority to and the benefit of U.S. Provisional Patent Application No. 63/638,100, filed on Apr. 24, 2024, entitled “Carbon Capture System and Method for Synthetic Turf Fields”, which we incorporate by reference in its entirety.\|(US20250333914)\|BACKGROUND\|[0002] Synthetic or artificial turf fields are composed of three primary components—from bottom to top: Shock pad, carpet, and infill. These components are generally assembled on top of a base of compacted stone. The shock pad is optional and serves to convey much of the shock absorption performance of the turf field, required for the safety of those playing on the surface in the case of impact with the surface. The carpet serves to mimic the blades of grass and root zone, conveying the softness and traction of the surface as well as many of the ball interaction properties. The infill is generally constituted of at least two layers, the bottom layer of which serves to weight down and stabilize the carpets that it is laid onto, whereas the top layers serve as an additional interface layer to those playing on the field, conveying surface softness, friction, traction, and much of the mechanical properties of the field that are felt directly by the players.\|[0003] When installation of a synthetic turf field occurs, generally speaking, a living, natural turf field is being replaced with an artificial one. In this process, a living organism, e.g., grass, plants, etc., which naturally removes carbon dioxide from the atmosphere is removed. Additionally, the construction associated with a synthetic turf field, as well as the actual manufacturing of the synthetic turf, result in additional carbon entering the atmosphere.\|SUMMARY\|[0004] The following presents a simplified summary to provide a basic understanding of some aspects of the disclosed subject matter. This summary is not an extensive overview. It is not intended to identify key/critical elements or to delineate the scope of the claimed subject matter. Its sole purpose is to present some concepts in a simplified form as a prelude to the more detailed description presented later.\|[0005] There remains a need for environmentally friendly and ultimately carbon-neutral or carbon-offsetting materials that present good mechanical properties and mechanical resistance, while presenting high availability, easy transportation, and low cost.\|[0006] In aspects, a rock dust-based layer may be positioned immediately below the installation of an synthetic turf system, e.g., below a shock pad, on a top substrate material, e.g., a rock layer. In such a position, the rock dust-based layer may have a thickness of ⅛″ to ¼″.\|[0007] In still other aspects, rock dust-based particles may be blended into a 1″ to 2″ topping stone layer positioned immediately below the shock pad.\|[0008] In yet another aspect, a layer of rock dust-based particles may be positioned on a geotextile or subgrade layer. In such a position, the rock dust-based layer may have a thickness of ¼″ to ½″.\|[0009] In another aspect, a rock dust-based material may be positioned at a bottom of a subdrain trench, below a layer of geotextile fabric.\|[0010] In a further aspect, rock dust-based particles may be tilled or blended into native subgrade material. In such a position, the rock dust-based particles may be blended within the subgrade, e.g., soil, as discussed below.\|[0011] In another aspect, a synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes rock dust, or the synthetic turf system further includes a layer of the rock dust disposed above or below the one or more infill layers. The rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.\|[0012] In another aspect, infill for a synthetic turf system includes rock dust. The rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater. At least 90 percent of the rock dust has a particle size less than 250 micrometers. Organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust in one or more infill layers.\|[0013] In another aspect, a method of preparing a synthetic turf system includes dispersing rock dust over a top portion of turf fibers. The rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|[0014] In each of the foregoing aspects, certain carbon sequestration processes can occur as rainwater interacts with the rock dust-based particles, regardless of the position in the synthetic turf system. Further discussion of the processes referenced above are included in the following description.\|[0015] To the accomplishment of the foregoing and related ends, certain illustrative aspects of the claimed subject matter are described herein in connection with the following description and the annexed drawings. These aspects indicate various ways in which the subject matter may be practiced, all of which are intended to be within the scope of the disclosed subject matter. Other advantages and novel features may become apparent from the following detailed description when considered in conjunction with the drawings.\|[0016] These and other systems, methods, objects, features, and advantages of the present disclosure will be apparent to those skilled in the art from the following detailed description of the preferred embodiment and the drawings.\|[0017] All documents mentioned herein are hereby incorporated in their entirety by reference. References to items in the singular should be understood to include items in the plural, and vice versa, unless explicitly stated otherwise or clear from the text. Grammatical conjunctions are intended to express any and all disjunctive and conjunctive combinations of conjoined clauses, sentences, words, and the like, unless otherwise stated or clear from the context.\|(US20250333914)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] FIG. 1 is a partial perspective view of an example synthetic turf system having an infill made of rock dust in accordance with some embodiments of the present disclosure.\|[0019] FIG. 2 is a perspective view of an example application system employed in dispersing the rock dust over the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0020] FIG. 3 is a perspective view of an example brush employed in grooming the rock dust into the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0021] FIG. 4 is a partial perspective view of an example synthetic turf system having rock dust applied to a top surface of a base stone layer in accordance with some embodiments.\|[0022] FIG. 5 is a partial perspective view of an example synthetic turf system having rock dust incorporated into a base stone layer in accordance with some embodiments.\|[0023] FIG. 6 is a partial perspective view of an example synthetic turf system having the rock dust positioned on a geotextile component in accordance with some embodiments.\|[0024] FIG. 7 is a partial perspective view of an example synthetic turf system having rock dust positioned in a subdrain trench in accordance with some embodiments.\|[0025] FIG. 8 is a partial perspective view of an example synthetic turf system having rock dust diffused into a subgrade in accordance with some embodiments.\|[0026] FIG. 9 is an example process flow for preparing a synthetic turf system.\|(US20250333914)\|DETAILED DESCRIPTION\|[0027] Various aspects of the subject disclosure are now described in more detail with reference to the annexed drawings, wherein like numerals generally refer to like or corresponding elements throughout. It should be understood, however, that the drawings and detailed description relating thereto are not intended to limit the claimed subject matter to the particular form disclosed. Instead, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the described and claimed subject matter.\|[0028] The following disclosure provides many different embodiments, or examples, for implementing different features of the provided subject matter. Specific examples of components and arrangements are described below to simplify the present disclosure. These are, of course, merely examples and are not intended to be limiting. For example, the formation of a first feature over or on a second feature in the description that follows may include embodiments in which the first and second features are formed in direct contact, and may also include embodiments in which additional features may be formed between the first and second features, such that the first and second features may not be in direct contact. In addition, the present disclosure may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.\|[0029] Further, spatially relative terms, such as “beneath,” “below,” “lower,” “above,” “upper” and the like, may be used herein for ease of description to describe one element or feature's relationship to another element(s) or feature(s) as illustrated in the figures. The spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. The apparatus may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein may likewise be interpreted accordingly.\|[0030] Numerical values in the specification and claims of this application should be understood to include numerical values which are the same when reduced to the same number of significant figures and numerical values which differ from the stated value by less than the experimental error of conventional measurement technique of the type described in the present application to determine the value. All ranges disclosed herein are inclusive of the recited endpoint.\|[0031] The term “about” can be used to include any numerical value that can vary without changing the basic function of that value. When used with a range, “about” also discloses the range defined by the absolute values of the two endpoints, e.g., “about 2 to about 4” also discloses the range “from 2 to 4.” For example, the term “about” may refer to plus or minus 10% of the indicated number.\|[0032] In accordance with some aspects described herein, there is provided an synthetic turf system that utilizes a material derived from one or more types of rock dust, including, for example and without limitation, basalt rock dust, igneous rock dust (such as andesite, diorite, gabbro, or rhyolite), limestone-derived dust (such as calcium carbonate-based materials), dolomitic lime (CaO/MgO), ultramafic rock dust (such as peridotite or dunite), industrial byproducts containing reactive silicates or carbonates, a blend of various types of rock dust, combinations thereof, or other similar mineral-based particulate materials. In some embodiments, the rock dust may be used as an intervening layer of material between existing layers of the system, mixed within a particular layer, lining a subdrain trench, on or mixed within a substrate, or combinations thereof. It will further be appreciated that as the rock dust is a natural byproduct of the mining industry, there is no additional carbon footprint from mining.\|[0033] In some embodiments contemplated herein, the rock dust material, when in contact with rainwater, causes a chemical reaction to occur between carbonic acid naturally present in the rainwater and the rock dust. The reaction weathers the rock dust and converts the carbonic acid into a carbonate or bicarbonate. By converting the carbon dioxide into other substances, the carbon dioxide can no longer be released into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These carbonate or bicarbonate substances are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments. These carbonate sediments form a sink for carbon dioxide.\|[0034] Turning now to FIG. 1, there is shown a three-dimensional cross-sectional view of a portion of an synthetic turf system 100 utilizing rock dust 102 for carbon sequestration in accordance with an example implementation of the embodiment described above. As shown in FIG. 1, the synthetic turf system 100 includes one or more infill layers 104, a backing 110, and a plurality of turf fibers 112 that emulate grass blades extending substantially perpendicularly upwards relative to the backing 110. As such, the infill layers 104 are positioned above the backing 110, in between the turf fibers 112, and below a top portion 114 of the turf fibers 112.\|[0035] Infill, as shown in FIG. 1, is representative of material that is deposited directly on top of the backing 110 and forms the infill layers 104 around the turf fibers 112. Infill is interspersed between the turf fibers 112, rising out of the backing 110. As depicted, the infill layers 104 have a total depth that covers a portion of the turf fibers 112, leaving at least part of the top portion 114 exposed and extending above the infill layers 104.\|[0036] In accordance with some embodiments, the infill layers 104 assist in supporting the turf fibers 112 in an upright position from the backing 110, and provide traction and shock absorption. As a general matter, various types of infill arrangements are contemplated. In this regard, the one or more infill layers 104 may be a single homogeneous or graded layer, or a plurality of distinct layers. For example, two layer, three layer, or other further layered arrangements of the one or more infill layers 104 are contemplated. For convenience, the present description primarily discusses two and three layer embodiments.\|[0037] In some embodiments, a first layer 120 of infill material may include, for example and without limitation, styrene-butadiene rubber (SBR) particles ethylene propylene diene monomer (EPDM) rubber, other thermoplastics such as polyvinyl chloride (PVC), composite materials can be used that combine thermoplastics, elastomers, reinforcements and/or fillers or other sufficient material, is incorporated. In accordance with some embodiments, a second layer 122 of infill material depicted in FIG. 1 may include a mixture of materials, e.g., material of the first layer 104 and a sand material. In such embodiments, a third layer 124 of infill material may include the aforementioned sand material, which may be implemented as a ballast layer.\|[0038] In accordance with some embodiments, a shock pad (not shown) may be employed to achieve a desired shock absorption in accordance with a particular installation/purpose. For example, a shock pad (not shown) may be positioned below the one or more infill layers 104 shown in FIG. 1. As such, the material of the infill layers 104 conveys many of the mechanical properties that may be desired for use as artificial turf infill. As shown in the depicted embodiment, the backing 110 may be positioned below the infill layers 104 shown in FIG. 1. In such embodiments, the permeable backing may correspond to the material into which the turf fibers 112 are woven, held, inserted, etc.\|[0039] In an embodiment where the rock dust 102 is incorporated in the synthetic turf system 100 as a top dressing, the rock dust 102 is periodically dispersed over the top portion 114 of the turf fibers 112 with an application system 130 depicted in FIG. 2. With continued reference to FIG. 2, the application system 130 includes a seed tender 132 and a tractor 134 that disperses the rock dust 102 over the synthetic turf system 100 from a broadcaster tool 140. The seed tender 132 is employed in conjunction with a hydraulically-controlled conveyor 142 and a hopper gate 144, which supply the tractor 134 the rock dust 102. As the tractor 134 moves at a consistent speed across the synthetic turf system 100 following a predetermined pattern, the hydraulically-controlled conveyor 142 and the hopper gate 144 precisely control a flow rate of the rock dust 102 to the tractor 134, ensuring uniform distribution across the synthetic turf system 100.\|[0040] While, as depicted, the application system 130 includes the broadcaster tool 140 pulled by the tractor 134, and continuously fed the rock dust 102 by the seed tender 132 along or across the synthetic turf system 100, the application system 130 may additionally or alternatively include a variety of components configured to spread granular material across a field, such as, for example, a self-propelled, manually powered, or power take-off (PTO) driven broadcast material spreader, a pneumatic spreader, an air boom spreader, a drop spreader, a handheld spreader, or an aerial spreader for dispersing the rock dust 102 without departing from the scope of the present disclosure.\|[0041] Once the rock dust 102 is dispersed across the synthetic turf system 100 by the application system 130, the rock dust 102 is brushed into the one or more infill layers 104, including the first layer 120, the second layer 122, and the third layer 124. In this regard, a brush 150 depicted in FIG. 3 grooms the rock dust 102 into the one or more infill layers 104. Rotary brush action on the synthetic turf system 100 from the top portion 114 by the brush 150 effectively works the rock dust 102 downward between the turf fibers 112, ensuring proper placement within the infill material forming the one or more infill layers 104, while maintaining structural integrity and performance characteristics of the synthetic turf system 100, including at the top portion 114 and the first layer 120.\|[0042] While, as depicted, the brush 150 is a motorized, walk-behind rotary brush apparatus, such as a Shindaiwa or Laymor brush system, the brush 150 may additionally or alternatively include various components for incorporating the rock dust 102 into the one or more infill layers 104 such as, for example, a ride-on turf groomer, a tractor-mounted brush that is dragged or PTO driven, or manual turf brushing equipment. Furthermore, brushes employed in such configurations may embody various shapes, sizes, and types, such as, for example, straight brushes, triangular brushes, hydraulic brushes, oscillating brushes, rigid brushes, flexible brushes, or brush assemblies including at least one plurality of brushes. Furthermore, the brush 150 may additionally or alternatively include specialty turf equipment, such as a vacuum or other devices complementary to the brush 150, and utilized to integrate the rock dust 102 into the existing infill material of the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0043] Turning now to FIG. 4, there is shown a more detailed three-dimensional cross-sectional view of a portion of the synthetic turf system 100 utilizing the rock dust 102 as a ballast infill material in accordance with the embodiment set forth above in FIG. 1. It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the rock dust 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-7 are intended solely as one non-limiting example of turf carpet systems in which the rock dust 102 may be utilized.\|[0044] As shown in FIG. 4, the synthetic turf system 100, in addition to including the turf fibers 112, the rock dust 102, the infill layers 104, and the backing 110, further includes a first base stone layer 200 disposed below the backing 110 and above a second base stone layer 202. The synthetic turf system 100 further includes a geotextile component 204 that is a fabric disposed between the second base stone layer 202 and a subgrade 210. The synthetic turf system 100 may further include a subdrain trench component 212 formed in the subgrade and housing a drainage pipe 214.\|[0045] The synthetic turf system 100 may include the rock dust 102 in the infill layers 104, or further include a layer of the rock dust 102 disposed above or below the one or more infill layers 104. In the embodiment of FIG. 4, the rock dust 102 is applied to a top surface of the first base stone layer 200, below the backing 110 and the shock pad. More specifically, the rock dust 102 is layered directly on the top surface of the first base stone layer 200, and forms a continuous layer along the backing 110, where the layer of the rock dust 102 has a thickness of at least one eighth of an inch. Application may be made via a suitable top-dressing machine, as described above. In an embodiment, the rock dust 102 may be deposited with a thickness in the range of about ⅛″ to ¼″. In such an embodiment, rainwater would flow directly through the infill layers 104, the backing 110, and the rock dust 102, and flow into the first base stone layer 200.\|[0046] The rock dust 102 is accessible to rainwater from the top portion 114 of the turf fibers 112, where the rainwater and the rock dust 102 chemically react with each other, forming a carbonate or a bicarbonate. More specifically, in operation, as rainwater contacts the rock dust 102, a chemical reaction occurs between carbonic acid naturally present in the rainwater and the rock dust. The reaction weathers the rock dust 102, e.g., silicate rock, igneous rock, or other reactive rock, rock blends, combinations thereof, etc., and converts the carbonic acid into a carbonate or bicarbonate. In this regard, the rock dust 102 may include wollastonite, basalt, peridotite, dunite, dolomitic lime, dolostone, andesite, diorite, gabbro, rhyolite, olivine, quick lime, lime stone, and other minerals in varying proportions effective for reacting with carbonic acid in rainwater.\|[0047] The weathering rate and shape of particles forming the rock dust 102 are influenced by material selection and particle size distribution. In this regard, consistent particle sizing promotes uniform weathering rates across the one or more infill layers 104, maintaining overall field performance and carbon sequestration efficiency in the synthetic turf system 100. The rock dust 102 is accessible to rainwater traveling downward by gravity from the top portion 114 of the turf fibers 112 toward the backing 110. As the rock dust 102 weathers through exposure to rainwater, its constituent particles may substantially change morphology, or alternatively may remain largely the same shape. In embodiments, the selected silicate rock, igneous rock, or reactive rock materials form weathered particles that maintain a sphericity of about 0.65 to about 0.85. This sphericity range supports stable packing within the synthetic turf system, reduces compaction variability, and ensures continued mechanical performance while facilitating consistent chemical reactions for carbon capture.\|[0048] The rock dust 102 has a particle size distribution that optimizes contact surface area and reactivity with rainwater, without preventing drainage of the rainwater from the synthetic turf system 100. In this regard, a majority of the particles forming the rock dust 102 may be silt, very fine sand, or fine sand in accordance with the Wentworth aggregate classification scheme. In such an embodiment, for example, at least 90 percent of the rock dust 102 by weight may have a particle size greater than 4 micrometers and less than 250 micrometers. In a further embodiment, at least 90 percent of the rock dust 102 by weight may have a particle size less than 125 micrometers. In a further embodiment, at least 90 percent of the rock dust 102 by weight may have a particle size less than 62 micrometers.\|[0049] The infill material forming the infill layers 104 may also include additional materials such as organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust 102. In an embodiment, the rock dust 102 forms less than 10 percent of the infill by weight, as compared to the additional materials. In such an embodiment, the additional materials may be sized and shaped to provide an engineered drainage surface in the synthetic turf system 100, where the rock dust 102 reacts with rainwater without forming an impermeable barrier in the infill layers 104 or otherwise effectively blocking, clogging, or pooling flow of rainwater through the synthetic turf system 100.\|[0050] As stated above, the conversion of the carbon dioxide into other substances, such as carbonate and bicarbonate substances prevents the release of the carbon dioxide into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These carbonate or bicarbonate substances permeate the first base stone layer 200 and the second base stone layer 202, through the geotextile component 204 and into the subdrain trench component 212 and drainage pipe 214. Thereafter, the carbonate or bicarbonate substances are carried by rivers to the sea, where they are ultimately deposited as carbonate sediments such as limestone and dolomites, forming a sink for carbon dioxide.\|[0051] Turning now to FIG. 5, there is shown the synthetic turf system 100 utilizing the rock dust 102 in accordance with another embodiment. In the embodiment depicted in FIG. 5, the rock dust 102 is incorporated into the first base stone layer 200. In accordance with one non-limiting example, the first base stone layer 200 may be implemented as layer of stone having a thickness in the range of about 1 inch to 4 inches, and in some particular embodiments, in the range of about 1 inch to about 2 inches. In such embodiments, the first base stone layer 200 may include ASTM #89 stone or the like. The rock dust 102 may be suitably mixed with the stone to distribute the rock dust 102 throughout the first base stone layer 200. Mixing of the rock dust 102 with the first base stone layer 200 may be accomplished on-site, remotely, e.g., quarry, mine, etc., or the like. As described in greater detail above, reaction of the rock dust 102 with rainwater would occur as described above with respect to FIGS. 1 and 4.\|[0052] Turning now to FIG. 6, there is shown another embodiment of the synthetic turf system 100 utilizing the rock dust 102. As illustrated in FIG. 6, the rock dust 102 is disposed or layered on the geotextile component 204. In such a position, the layer of the rock dust 102 disposed on the geotextile component 204 may have a thickness of ¼″ to ½″. Stated another way, the layer of the rock dust 102 may be applied at the bottom of the second base stone layer 202, as shown in FIG. 6. Application of the layer of the rock dust 102 in FIG. 6 may be accomplished, for example and without limitation, via a suitable top-dressing machine.\|[0053] In accordance with one non-limiting example, the second base stone layer 202 may be implemented as layer of stone having a thickness in the range of about 2 inch to 6 inches, and in some particular embodiments, in the range of about 3 inches to about 4 inches. In such embodiments, the second base stone layer 202 may include ASTM #57 stone or the like. In this manner, the first base stone layer 200 is formed from stone having a first nominal size range, the second base stone layer 202 disposed below the first base stone layer 200 has a second nominal size range coarser than the first nominal size range, and the rock dust 102 is layered above, layered below, or mixed the first base stone layer 200 or the second base stone layer 202. Further, with this construction, the first base stone layer 200 and the second base stone layer 202 are water permeable, and the rock dust 102 is accessible by rainwater traveling from the top portion 114 of the turf fibers 112, through the one or more infill layers 104 by gravity\|[0054] Further, reaction of rock dust 102 with rainwater would occur as described above with respect to FIGS. 1, 4, and 5. It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|[0055] Referring now to FIG. 7, there is shown another embodiment of the synthetic turf system 100 utilizing rock dust 102 for carbon sequestration. As illustrated in FIG. 7, a layer of the rock dust 102 is positioned at a bottom of the subdrain trench component 212. In such an embodiment, the rock dust 102 may be placed at the lowest elevation within the system 100 to maximize the possibility of water coming into contact with the rock dust 102. In some embodiments, although not shown, the rock dust 102 may also be placed below the geotextile component 204, preventing the rock dust 102 from clogging up the drainage system at or between the geotextile component 204 and the subdrain trench component 212, or from being washed down stream. Accordingly, the elevation of the drainage pipe 214 as a storm drain outlet may be utilized to maximize the contact time with the storm water, effectively maximizing the weathering and carbon dioxide capture of the rock dust 102.\|[0056] Although not shown, it is contemplated that the rock dust 102 may be blended with the stone of the second base stone layer 202 similar to the manner described above with respect to FIGS. 1 and 4-6. Similarly, although not illustrated in the accompanying figures, it is further contemplated that the rock dust 102 may be blended with stone in the subdrain trench component 212. The above described positions of the rock dust 102 would also enable the carbon capture reaction described above with respect to FIGS. 1 and 4-6.\|[0057] Referring now to FIG. 8, there is shown the synthetic turf system 100 utilizing rock dust 102 in accordance with another embodiment. As illustrated in FIG. 8, the rock dust 102 may be tilled and incorporated into the subgrade 210 of the synthetic turf system 100, e.g., soil, sediment, etc. In such an implementation, the geotextile component 204 and the 6″ to 8″ combined thickness of the first base stone layer 200 and the second base stone layer 202 may be installed on the modified subgrade 210 having the rock dust 102 distributed therein. It will be appreciated that more rock dust 102 may be used with this embodiment than the embodiments described above, thereby providing additional carbon sequestration capability. Furthermore, it will be appreciated that by placing the rock dust 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air. That is, as organic matter breaks down it creates additional carbon dioxide. Furthermore, the addition of rock dust 102 in the subgrade 210, in addition to carbon sequestration, may also provide firmer and more permeable subgrade, particularly if the subgrade 210 is formed of soft, silty, or sandy soils. Having rock dust 102 in the subgrade 210 where there is potential for more water availability increases the ability for the weathering reaction to occur, e.g., carbon sequestration. In addition, as described above with respect to FIGS. 1 and 4-7, rainwater reaction with the rock dust 102 provides the aforementioned carbon capture benefits.\|[0058] Referring to FIG. 9, a method 300 for preparing a synthetic turf system will be described according to an exemplary embodiment. FIG. 9 will be described with reference to FIGS. 1-8. For simplicity, the method 300 will be described as a sequence of blocks, but the elements of the method 300 can be organized into different architectures, elements, stages, and/or processes.\|[0059] At block 302, the method 300 includes measuring an aspect of the synthetic turf system 100. More specifically, a user may measure a thickness of an infill layer, such as one of the infill layers 104, may measure an acidity of rainwater at the infill layer, and may measure a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer.\|[0060] At block 304, the method 300 includes preblending or layering the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the rock dust 102 over the top portion 114 of the turf fibers 112. In an embodiment, the method 300 includes determining desired compositional ranges of the rock dust 102 based on the measurement or measurements taken at block 302. In this manner, the wear rate and the minimum volume of the one or more infill layers 104 is controlled by adjusting the compositional ranges of components of the rock dust 102. In an embodiment, the rock dust 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0061] At block 310, the method 300 includes dispersing the rock dust 102 over the top portion 114 of the turf fibers 112, where the rock dust 102 includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through the one or more infill layers 104 by gravity. In an embodiment, dispersing the rock dust 102 includes dispersing a predetermined quantity of the rock dust 102 over the top portion 114 of the turf fibers 112 as a top dressing based on the measurement taken at block 302.\|[0062] At block 312, the method 300 includes grooming the rock dust 102 into the one or more infill layers 104 of the synthetic turf system 100, between the turf fibers 112, at the backing 110 of the synthetic turf system 100. In this regard, the brush 150 grooms the rock dust 102 into and through the one or more infill layers 104, where the rock dust 102 contacts and rests on the backing 110.\|[0063] While specific embodiments are shown and described herein, it is contemplated that alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc. without departing from the spirit and/or scope of the innovation as described in detail. These alternative embodiments are to be included within the spirit and scope of the innovation as described and claimed herein.\|[0064] Although the subject matter has been described in language specific to structural features or methodological acts, it is to be understood that the subject matter of the appended claims is not necessarily limited to the specific features or acts described above. Rather, the specific features and acts described above are disclosed as example aspects.\|[0065] Various operations of aspects are provided herein. The order in which one or more or all of the operations are described should not be construed as to imply that these operations are necessarily order dependent. Alternative ordering will be appreciated based on this description. Further, not all operations may necessarily be present in each aspect provided herein.\|[0066] As used in this application, “or” is intended to mean an inclusive “or” rather than an exclusive “or”. Further, an inclusive “or” may include any combination thereof (e.g., A, B, or any combination thereof). In addition, “a” and “an” as used in this application are generally construed to mean “one or more” unless specified otherwise or clear from context to be directed to a singular form. Additionally, at least one of A and B and/or the like generally means A or B or both A and B. Further, to the extent that “includes”, “having”, “has”, “with”, or variants thereof are used in either the detailed description or the claims, such terms are intended to be inclusive in a manner similar to the term “comprising”.\|[0067] Further, unless specified otherwise, “first”, “second”, or the like are not intended to imply a temporal aspect, a spatial aspect, an ordering, etc. Rather, such terms are merely used as identifiers, names, etc. for features, elements, items, etc. For example, a first channel and a second channel generally correspond to channel A and channel B or two different or two identical channels or the same channel. Additionally, “comprising”, “comprises”, “including”, “includes”, or the like generally means comprising or including, but not limited thereto.\|[0068] Further, the term “in” as used to describe an object with respect to a given direction (e.g., an edge extended in a left-right direction) is intended to denote an orientation that is substantially parallel to the specified direction. In contrast, the term “along” as used to describe an object with respect to a given direction (e.g., an edge extended along a vertical direction) is intended to indicate that a feature or element possesses a common vector component in that direction, even if its overall alignment is not strictly parallel.\|[0069] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions and/or alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc., do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.	(US20250333914)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] The application claims priority to and the benefit of U.S. Provisional Patent Application No. 63/638,100, filed on Apr. 24, 2024, entitled “Carbon Capture System and Method for Synthetic Turf Fields”, which we incorporate by reference in its entirety.\|(US20250333914)\|BACKGROUND\|[0002] Synthetic or artificial turf fields are composed of three primary components—from bottom to top: Shock pad, carpet, and infill. These components are generally assembled on top of a base of compacted stone. The shock pad is optional and serves to convey much of the shock absorption performance of the turf field, required for the safety of those playing on the surface in the case of impact with the surface. The carpet serves to mimic the blades of grass and root zone, conveying the softness and traction of the surface as well as many of the ball interaction properties. The infill is generally constituted of at least two layers, the bottom layer of which serves to weight down and stabilize the carpets that it is laid onto, whereas the top layers serve as an additional interface layer to those playing on the field, conveying surface softness, friction, traction, and much of the mechanical properties of the field that are felt directly by the players.\|[0003] When installation of a synthetic turf field occurs, generally speaking, a living, natural turf field is being replaced with an artificial one. In this process, a living organism, e.g., grass, plants, etc., which naturally removes carbon dioxide from the atmosphere is removed. Additionally, the construction associated with a synthetic turf field, as well as the actual manufacturing of the synthetic turf, result in additional carbon entering the atmosphere.\|SUMMARY\|[0004] The following presents a simplified summary to provide a basic understanding of some aspects of the disclosed subject matter. This summary is not an extensive overview. It is not intended to identify key/critical elements or to delineate the scope of the claimed subject matter. Its sole purpose is to present some concepts in a simplified form as a prelude to the more detailed description presented later.\|[0005] There remains a need for environmentally friendly and ultimately carbon-neutral or carbon-offsetting materials that present good mechanical properties and mechanical resistance, while presenting high availability, easy transportation, and low cost.\|[0006] In aspects, a rock dust-based layer may be positioned immediately below the installation of an synthetic turf system, e.g., below a shock pad, on a top substrate material, e.g., a rock layer. In such a position, the rock dust-based layer may have a thickness of ⅛″ to ¼″.\|[0007] In still other aspects, rock dust-based particles may be blended into a 1″ to 2″ topping stone layer positioned immediately below the shock pad.\|[0008] In yet another aspect, a layer of rock dust-based particles may be positioned on a geotextile or subgrade layer. In such a position, the rock dust-based layer may have a thickness of ¼″ to ½″.\|[0009] In another aspect, a rock dust-based material may be positioned at a bottom of a subdrain trench, below a layer of geotextile fabric.\|[0010] In a further aspect, rock dust-based particles may be tilled or blended into native subgrade material. In such a position, the rock dust-based particles may be blended within the subgrade, e.g., soil, as discussed below.\|[0011] In another aspect, a synthetic turf system includes a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes rock dust, or the synthetic turf system further includes a layer of the rock dust disposed above or below the one or more infill layers. The rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.\|[0012] In another aspect, infill for a synthetic turf system includes rock dust. The rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater. At least 90 percent of the rock dust has a particle size less than 250 micrometers. Organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust in one or more infill layers.\|[0013] In another aspect, a method of preparing a synthetic turf system includes dispersing rock dust over a top portion of turf fibers. The rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|[0014] In each of the foregoing aspects, certain carbon sequestration processes can occur as rainwater interacts with the rock dust-based particles, regardless of the position in the synthetic turf system. Further discussion of the processes referenced above are included in the following description.\|[0015] To the accomplishment of the foregoing and related ends, certain illustrative aspects of the claimed subject matter are described herein in connection with the following description and the annexed drawings. These aspects indicate various ways in which the subject matter may be practiced, all of which are intended to be within the scope of the disclosed subject matter. Other advantages and novel features may become apparent from the following detailed description when considered in conjunction with the drawings.\|[0016] These and other systems, methods, objects, features, and advantages of the present disclosure will be apparent to those skilled in the art from the following detailed description of the preferred embodiment and the drawings.\|[0017] All documents mentioned herein are hereby incorporated in their entirety by reference. References to items in the singular should be understood to include items in the plural, and vice versa, unless explicitly stated otherwise or clear from the text. Grammatical conjunctions are intended to express any and all disjunctive and conjunctive combinations of conjoined clauses, sentences, words, and the like, unless otherwise stated or clear from the context.\|(US20250333914)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] FIG. 1 is a partial perspective view of an example synthetic turf system having an infill made of rock dust in accordance with some embodiments of the present disclosure.\|[0019] FIG. 2 is a perspective view of an example application system employed in dispersing the rock dust over the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0020] FIG. 3 is a perspective view of an example brush employed in grooming the rock dust into the synthetic turf system of FIG. 1, in accordance with some embodiments of the present disclosure.\|[0021] FIG. 4 is a partial perspective view of an example synthetic turf system having rock dust applied to a top surface of a base stone layer in accordance with some embodiments.\|[0022] FIG. 5 is a partial perspective view of an example synthetic turf system having rock dust incorporated into a base stone layer in accordance with some embodiments.\|[0023] FIG. 6 is a partial perspective view of an example synthetic turf system having the rock dust positioned on a geotextile component in accordance with some embodiments.\|[0024] FIG. 7 is a partial perspective view of an example synthetic turf system having rock dust positioned in a subdrain trench in accordance with some embodiments.\|[0025] FIG. 8 is a partial perspective view of an example synthetic turf system having rock dust diffused into a subgrade in accordance with some embodiments.\|[0026] FIG. 9 is an example process flow for preparing a synthetic turf system.\|(US20250333914)\|DETAILED DESCRIPTION\|[0027] Various aspects of the subject disclosure are now described in more detail with reference to the annexed drawings, wherein like numerals generally refer to like or corresponding elements throughout. It should be understood, however, that the drawings and detailed description relating thereto are not intended to limit the claimed subject matter to the particular form disclosed. Instead, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the described and claimed subject matter.\|[0028] The following disclosure provides many different embodiments, or examples, for implementing different features of the provided subject matter. Specific examples of components and arrangements are described below to simplify the present disclosure. These are, of course, merely examples and are not intended to be limiting. For example, the formation of a first feature over or on a second feature in the description that follows may include embodiments in which the first and second features are formed in direct contact, and may also include embodiments in which additional features may be formed between the first and second features, such that the first and second features may not be in direct contact. In addition, the present disclosure may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.\|[0029] Further, spatially relative terms, such as “beneath,” “below,” “lower,” “above,” “upper” and the like, may be used herein for ease of description to describe one element or feature's relationship to another element(s) or feature(s) as illustrated in the figures. The spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. The apparatus may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein may likewise be interpreted accordingly.\|[0030] Numerical values in the specification and claims of this application should be understood to include numerical values which are the same when reduced to the same number of significant figures and numerical values which differ from the stated value by less than the experimental error of conventional measurement technique of the type described in the present application to determine the value. All ranges disclosed herein are inclusive of the recited endpoint.\|[0031] The term “about” can be used to include any numerical value that can vary without changing the basic function of that value. When used with a range, “about” also discloses the range defined by the absolute values of the two endpoints, e.g., “about 2 to about 4” also discloses the range “from 2 to 4.” For example, the term “about” may refer to plus or minus 10% of the indicated number.\|[0032] In accordance with some aspects described herein, there is provided an synthetic turf system that utilizes a material derived from one or more types of rock dust, including, for example and without limitation, basalt rock dust, igneous rock dust (such as andesite, diorite, gabbro, or rhyolite), limestone-derived dust (such as calcium carbonate-based materials), dolomitic lime (CaO/MgO), ultramafic rock dust (such as peridotite or dunite), industrial byproducts containing reactive silicates or carbonates, a blend of various types of rock dust, combinations thereof, or other similar mineral-based particulate materials. In some embodiments, the rock dust may be used as an intervening layer of material between existing layers of the system, mixed within a particular layer, lining a subdrain trench, on or mixed within a substrate, or combinations thereof. It will further be appreciated that as the rock dust is a natural byproduct of the mining industry, there is no additional carbon footprint from mining.\|[0033] In some embodiments contemplated herein, the rock dust material, when in contact with rainwater, causes a chemical reaction to occur between carbonic acid naturally present in the rainwater and the rock dust. The reaction weathers the rock dust and converts the carbonic acid into a carbonate or bicarbonate. By converting the carbon dioxide into other substances, the carbon dioxide can no longer be released into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These carbonate or bicarbonate substances are carried by rivers to the sea, where they are ultimately deposited as limestone and dolomites, e.g., carbonate sediments. These carbonate sediments form a sink for carbon dioxide.\|[0034] Turning now to FIG. 1, there is shown a three-dimensional cross-sectional view of a portion of an synthetic turf system 100 utilizing rock dust 102 for carbon sequestration in accordance with an example implementation of the embodiment described above. As shown in FIG. 1, the synthetic turf system 100 includes one or more infill layers 104, a backing 110, and a plurality of turf fibers 112 that emulate grass blades extending substantially perpendicularly upwards relative to the backing 110. As such, the infill layers 104 are positioned above the backing 110, in between the turf fibers 112, and below a top portion 114 of the turf fibers 112.\|[0035] Infill, as shown in FIG. 1, is representative of material that is deposited directly on top of the backing 110 and forms the infill layers 104 around the turf fibers 112. Infill is interspersed between the turf fibers 112, rising out of the backing 110. As depicted, the infill layers 104 have a total depth that covers a portion of the turf fibers 112, leaving at least part of the top portion 114 exposed and extending above the infill layers 104.\|[0036] In accordance with some embodiments, the infill layers 104 assist in supporting the turf fibers 112 in an upright position from the backing 110, and provide traction and shock absorption. As a general matter, various types of infill arrangements are contemplated. In this regard, the one or more infill layers 104 may be a single homogeneous or graded layer, or a plurality of distinct layers. For example, two layer, three layer, or other further layered arrangements of the one or more infill layers 104 are contemplated. For convenience, the present description primarily discusses two and three layer embodiments.\|[0037] In some embodiments, a first layer 120 of infill material may include, for example and without limitation, styrene-butadiene rubber (SBR) particles ethylene propylene diene monomer (EPDM) rubber, other thermoplastics such as polyvinyl chloride (PVC), composite materials can be used that combine thermoplastics, elastomers, reinforcements and/or fillers or other sufficient material, is incorporated. In accordance with some embodiments, a second layer 122 of infill material depicted in FIG. 1 may include a mixture of materials, e.g., material of the first layer 104 and a sand material. In such embodiments, a third layer 124 of infill material may include the aforementioned sand material, which may be implemented as a ballast layer.\|[0038] In accordance with some embodiments, a shock pad (not shown) may be employed to achieve a desired shock absorption in accordance with a particular installation/purpose. For example, a shock pad (not shown) may be positioned below the one or more infill layers 104 shown in FIG. 1. As such, the material of the infill layers 104 conveys many of the mechanical properties that may be desired for use as artificial turf infill. As shown in the depicted embodiment, the backing 110 may be positioned below the infill layers 104 shown in FIG. 1. In such embodiments, the permeable backing may correspond to the material into which the turf fibers 112 are woven, held, inserted, etc.\|[0039] In an embodiment where the rock dust 102 is incorporated in the synthetic turf system 100 as a top dressing, the rock dust 102 is periodically dispersed over the top portion 114 of the turf fibers 112 with an application system 130 depicted in FIG. 2. With continued reference to FIG. 2, the application system 130 includes a seed tender 132 and a tractor 134 that disperses the rock dust 102 over the synthetic turf system 100 from a broadcaster tool 140. The seed tender 132 is employed in conjunction with a hydraulically-controlled conveyor 142 and a hopper gate 144, which supply the tractor 134 the rock dust 102. As the tractor 134 moves at a consistent speed across the synthetic turf system 100 following a predetermined pattern, the hydraulically-controlled conveyor 142 and the hopper gate 144 precisely control a flow rate of the rock dust 102 to the tractor 134, ensuring uniform distribution across the synthetic turf system 100.\|[0040] While, as depicted, the application system 130 includes the broadcaster tool 140 pulled by the tractor 134, and continuously fed the rock dust 102 by the seed tender 132 along or across the synthetic turf system 100, the application system 130 may additionally or alternatively include a variety of components configured to spread granular material across a field, such as, for example, a self-propelled, manually powered, or power take-off (PTO) driven broadcast material spreader, a pneumatic spreader, an air boom spreader, a drop spreader, a handheld spreader, or an aerial spreader for dispersing the rock dust 102 without departing from the scope of the present disclosure.\|[0041] Once the rock dust 102 is dispersed across the synthetic turf system 100 by the application system 130, the rock dust 102 is brushed into the one or more infill layers 104, including the first layer 120, the second layer 122, and the third layer 124. In this regard, a brush 150 depicted in FIG. 3 grooms the rock dust 102 into the one or more infill layers 104. Rotary brush action on the synthetic turf system 100 from the top portion 114 by the brush 150 effectively works the rock dust 102 downward between the turf fibers 112, ensuring proper placement within the infill material forming the one or more infill layers 104, while maintaining structural integrity and performance characteristics of the synthetic turf system 100, including at the top portion 114 and the first layer 120.\|[0042] While, as depicted, the brush 150 is a motorized, walk-behind rotary brush apparatus, such as a Shindaiwa or Laymor brush system, the brush 150 may additionally or alternatively include various components for incorporating the rock dust 102 into the one or more infill layers 104 such as, for example, a ride-on turf groomer, a tractor-mounted brush that is dragged or PTO driven, or manual turf brushing equipment. Furthermore, brushes employed in such configurations may embody various shapes, sizes, and types, such as, for example, straight brushes, triangular brushes, hydraulic brushes, oscillating brushes, rigid brushes, flexible brushes, or brush assemblies including at least one plurality of brushes. Furthermore, the brush 150 may additionally or alternatively include specialty turf equipment, such as a vacuum or other devices complementary to the brush 150, and utilized to integrate the rock dust 102 into the existing infill material of the one or more infill layers 104 without departing from the scope of the present disclosure.\|[0043] Turning now to FIG. 4, there is shown a more detailed three-dimensional cross-sectional view of a portion of the synthetic turf system 100 utilizing the rock dust 102 as a ballast infill material in accordance with the embodiment set forth above in FIG. 1. It will be appreciated that while illustrated in FIG. 4 as a multi-stone layered installation, the rock dust 102 may be used in other types of turf systems and in varying mesh sizes, and the illustrations in FIGS. 1-7 are intended solely as one non-limiting example of turf carpet systems in which the rock dust 102 may be utilized.\|[0044] As shown in FIG. 4, the synthetic turf system 100, in addition to including the turf fibers 112, the rock dust 102, the infill layers 104, and the backing 110, further includes a first base stone layer 200 disposed below the backing 110 and above a second base stone layer 202. The synthetic turf system 100 further includes a geotextile component 204 that is a fabric disposed between the second base stone layer 202 and a subgrade 210. The synthetic turf system 100 may further include a subdrain trench component 212 formed in the subgrade and housing a drainage pipe 214.\|[0045] The synthetic turf system 100 may include the rock dust 102 in the infill layers 104, or further include a layer of the rock dust 102 disposed above or below the one or more infill layers 104. In the embodiment of FIG. 4, the rock dust 102 is applied to a top surface of the first base stone layer 200, below the backing 110 and the shock pad. More specifically, the rock dust 102 is layered directly on the top surface of the first base stone layer 200, and forms a continuous layer along the backing 110, where the layer of the rock dust 102 has a thickness of at least one eighth of an inch. Application may be made via a suitable top-dressing machine, as described above. In an embodiment, the rock dust 102 may be deposited with a thickness in the range of about ⅛″ to ¼″. In such an embodiment, rainwater would flow directly through the infill layers 104, the backing 110, and the rock dust 102, and flow into the first base stone layer 200.\|[0046] The rock dust 102 is accessible to rainwater from the top portion 114 of the turf fibers 112, where the rainwater and the rock dust 102 chemically react with each other, forming a carbonate or a bicarbonate. More specifically, in operation, as rainwater contacts the rock dust 102, a chemical reaction occurs between carbonic acid naturally present in the rainwater and the rock dust. The reaction weathers the rock dust 102, e.g., silicate rock, igneous rock, or other reactive rock, rock blends, combinations thereof, etc., and converts the carbonic acid into a carbonate or bicarbonate. In this regard, the rock dust 102 may include wollastonite, basalt, peridotite, dunite, dolomitic lime, dolostone, andesite, diorite, gabbro, rhyolite, olivine, quick lime, lime stone, and other minerals in varying proportions effective for reacting with carbonic acid in rainwater.\|[0047] The weathering rate and shape of particles forming the rock dust 102 are influenced by material selection and particle size distribution. In this regard, consistent particle sizing promotes uniform weathering rates across the one or more infill layers 104, maintaining overall field performance and carbon sequestration efficiency in the synthetic turf system 100. The rock dust 102 is accessible to rainwater traveling downward by gravity from the top portion 114 of the turf fibers 112 toward the backing 110. As the rock dust 102 weathers through exposure to rainwater, its constituent particles may substantially change morphology, or alternatively may remain largely the same shape. In embodiments, the selected silicate rock, igneous rock, or reactive rock materials form weathered particles that maintain a sphericity of about 0.65 to about 0.85. This sphericity range supports stable packing within the synthetic turf system, reduces compaction variability, and ensures continued mechanical performance while facilitating consistent chemical reactions for carbon capture.\|[0048] The rock dust 102 has a particle size distribution that optimizes contact surface area and reactivity with rainwater, without preventing drainage of the rainwater from the synthetic turf system 100. In this regard, a majority of the particles forming the rock dust 102 may be silt, very fine sand, or fine sand in accordance with the Wentworth aggregate classification scheme. In such an embodiment, for example, at least 90 percent of the rock dust 102 by weight may have a particle size greater than 4 micrometers and less than 250 micrometers. In a further embodiment, at least 90 percent of the rock dust 102 by weight may have a particle size less than 125 micrometers. In a further embodiment, at least 90 percent of the rock dust 102 by weight may have a particle size less than 62 micrometers.\|[0049] The infill material forming the infill layers 104 may also include additional materials such as organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles blended or layered with the rock dust 102. In an embodiment, the rock dust 102 forms less than 10 percent of the infill by weight, as compared to the additional materials. In such an embodiment, the additional materials may be sized and shaped to provide an engineered drainage surface in the synthetic turf system 100, where the rock dust 102 reacts with rainwater without forming an impermeable barrier in the infill layers 104 or otherwise effectively blocking, clogging, or pooling flow of rainwater through the synthetic turf system 100.\|[0050] As stated above, the conversion of the carbon dioxide into other substances, such as carbonate and bicarbonate substances prevents the release of the carbon dioxide into the atmosphere. Further, the conversion of the carbonic acid has a de-acidifying effect on soils, storm water, rivers, and oceans, simultaneously enriching them with mineral nutrients. These carbonate or bicarbonate substances permeate the first base stone layer 200 and the second base stone layer 202, through the geotextile component 204 and into the subdrain trench component 212 and drainage pipe 214. Thereafter, the carbonate or bicarbonate substances are carried by rivers to the sea, where they are ultimately deposited as carbonate sediments such as limestone and dolomites, forming a sink for carbon dioxide.\|[0051] Turning now to FIG. 5, there is shown the synthetic turf system 100 utilizing the rock dust 102 in accordance with another embodiment. In the embodiment depicted in FIG. 5, the rock dust 102 is incorporated into the first base stone layer 200. In accordance with one non-limiting example, the first base stone layer 200 may be implemented as layer of stone having a thickness in the range of about 1 inch to 4 inches, and in some particular embodiments, in the range of about 1 inch to about 2 inches. In such embodiments, the first base stone layer 200 may include ASTM #89 stone or the like. The rock dust 102 may be suitably mixed with the stone to distribute the rock dust 102 throughout the first base stone layer 200. Mixing of the rock dust 102 with the first base stone layer 200 may be accomplished on-site, remotely, e.g., quarry, mine, etc., or the like. As described in greater detail above, reaction of the rock dust 102 with rainwater would occur as described above with respect to FIGS. 1 and 4.\|[0052] Turning now to FIG. 6, there is shown another embodiment of the synthetic turf system 100 utilizing the rock dust 102. As illustrated in FIG. 6, the rock dust 102 is disposed or layered on the geotextile component 204. In such a position, the layer of the rock dust 102 disposed on the geotextile component 204 may have a thickness of ¼″ to ½″. Stated another way, the layer of the rock dust 102 may be applied at the bottom of the second base stone layer 202, as shown in FIG. 6. Application of the layer of the rock dust 102 in FIG. 6 may be accomplished, for example and without limitation, via a suitable top-dressing machine.\|[0053] In accordance with one non-limiting example, the second base stone layer 202 may be implemented as layer of stone having a thickness in the range of about 2 inch to 6 inches, and in some particular embodiments, in the range of about 3 inches to about 4 inches. In such embodiments, the second base stone layer 202 may include ASTM #57 stone or the like. In this manner, the first base stone layer 200 is formed from stone having a first nominal size range, the second base stone layer 202 disposed below the first base stone layer 200 has a second nominal size range coarser than the first nominal size range, and the rock dust 102 is layered above, layered below, or mixed the first base stone layer 200 or the second base stone layer 202. Further, with this construction, the first base stone layer 200 and the second base stone layer 202 are water permeable, and the rock dust 102 is accessible by rainwater traveling from the top portion 114 of the turf fibers 112, through the one or more infill layers 104 by gravity\|[0054] Further, reaction of rock dust 102 with rainwater would occur as described above with respect to FIGS. 1, 4, and 5. It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|[0055] Referring now to FIG. 7, there is shown another embodiment of the synthetic turf system 100 utilizing rock dust 102 for carbon sequestration. As illustrated in FIG. 7, a layer of the rock dust 102 is positioned at a bottom of the subdrain trench component 212. In such an embodiment, the rock dust 102 may be placed at the lowest elevation within the system 100 to maximize the possibility of water coming into contact with the rock dust 102. In some embodiments, although not shown, the rock dust 102 may also be placed below the geotextile component 204, preventing the rock dust 102 from clogging up the drainage system at or between the geotextile component 204 and the subdrain trench component 212, or from being washed down stream. Accordingly, the elevation of the drainage pipe 214 as a storm drain outlet may be utilized to maximize the contact time with the storm water, effectively maximizing the weathering and carbon dioxide capture of the rock dust 102.\|[0056] Although not shown, it is contemplated that the rock dust 102 may be blended with the stone of the second base stone layer 202 similar to the manner described above with respect to FIGS. 1 and 4-6. Similarly, although not illustrated in the accompanying figures, it is further contemplated that the rock dust 102 may be blended with stone in the subdrain trench component 212. The above described positions of the rock dust 102 would also enable the carbon capture reaction described above with respect to FIGS. 1 and 4-6.\|[0057] Referring now to FIG. 8, there is shown the synthetic turf system 100 utilizing rock dust 102 in accordance with another embodiment. As illustrated in FIG. 8, the rock dust 102 may be tilled and incorporated into the subgrade 210 of the synthetic turf system 100, e.g., soil, sediment, etc. In such an implementation, the geotextile component 204 and the 6″ to 8″ combined thickness of the first base stone layer 200 and the second base stone layer 202 may be installed on the modified subgrade 210 having the rock dust 102 distributed therein. It will be appreciated that more rock dust 102 may be used with this embodiment than the embodiments described above, thereby providing additional carbon sequestration capability. Furthermore, it will be appreciated that by placing the rock dust 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air. That is, as organic matter breaks down it creates additional carbon dioxide. Furthermore, the addition of rock dust 102 in the subgrade 210, in addition to carbon sequestration, may also provide firmer and more permeable subgrade, particularly if the subgrade 210 is formed of soft, silty, or sandy soils. Having rock dust 102 in the subgrade 210 where there is potential for more water availability increases the ability for the weathering reaction to occur, e.g., carbon sequestration. In addition, as described above with respect to FIGS. 1 and 4-7, rainwater reaction with the rock dust 102 provides the aforementioned carbon capture benefits.\|[0058] Referring to FIG. 9, a method 300 for preparing a synthetic turf system will be described according to an exemplary embodiment. FIG. 9 will be described with reference to FIGS. 1-8. For simplicity, the method 300 will be described as a sequence of blocks, but the elements of the method 300 can be organized into different architectures, elements, stages, and/or processes.\|[0059] At block 302, the method 300 includes measuring an aspect of the synthetic turf system 100. More specifically, a user may measure a thickness of an infill layer, such as one of the infill layers 104, may measure an acidity of rainwater at the infill layer, and may measure a quantity of silicate rock, ultramafic rock, or reactive rock present in the infill layer.\|[0060] At block 304, the method 300 includes preblending or layering the silicate rock, ultramafic rock, or reactive rock with organic particles, rubber particles, elastomer particles, coated particles, or thermoplastic particles prior to dispersing the rock dust 102 over the top portion 114 of the turf fibers 112. In an embodiment, the method 300 includes determining desired compositional ranges of the rock dust 102 based on the measurement or measurements taken at block 302. In this manner, the wear rate and the minimum volume of the one or more infill layers 104 is controlled by adjusting the compositional ranges of components of the rock dust 102. In an embodiment, the rock dust 102 may be preblended or layered with wollastonite, olivine, limestone, or basalt, etc., and additional infill materials complementary to the one or more infill layers 104 for producing desired field conditions in the synthetic turf system 100.\|[0061] At block 310, the method 300 includes dispersing the rock dust 102 over the top portion 114 of the turf fibers 112, where the rock dust 102 includes silicate rock, ultramafic rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through the one or more infill layers 104 by gravity. In an embodiment, dispersing the rock dust 102 includes dispersing a predetermined quantity of the rock dust 102 over the top portion 114 of the turf fibers 112 as a top dressing based on the measurement taken at block 302.\|[0062] At block 312, the method 300 includes grooming the rock dust 102 into the one or more infill layers 104 of the synthetic turf system 100, between the turf fibers 112, at the backing 110 of the synthetic turf system 100. In this regard, the brush 150 grooms the rock dust 102 into and through the one or more infill layers 104, where the rock dust 102 contacts and rests on the backing 110.\|[0063] While specific embodiments are shown and described herein, it is contemplated that alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc. without departing from the spirit and/or scope of the innovation as described in detail. These alternative embodiments are to be included within the spirit and scope of the innovation as described and claimed herein.\|[0064] Although the subject matter has been described in language specific to structural features or methodological acts, it is to be understood that the subject matter of the appended claims is not necessarily limited to the specific features or acts described above. Rather, the specific features and acts described above are disclosed as example aspects.\|[0065] Various operations of aspects are provided herein. The order in which one or more or all of the operations are described should not be construed as to imply that these operations are necessarily order dependent. Alternative ordering will be appreciated based on this description. Further, not all operations may necessarily be present in each aspect provided herein.\|[0066] As used in this application, “or” is intended to mean an inclusive “or” rather than an exclusive “or”. Further, an inclusive “or” may include any combination thereof (e.g., A, B, or any combination thereof). In addition, “a” and “an” as used in this application are generally construed to mean “one or more” unless specified otherwise or clear from context to be directed to a singular form. Additionally, at least one of A and B and/or the like generally means A or B or both A and B. Further, to the extent that “includes”, “having”, “has”, “with”, or variants thereof are used in either the detailed description or the claims, such terms are intended to be inclusive in a manner similar to the term “comprising”.\|[0067] Further, unless specified otherwise, “first”, “second”, or the like are not intended to imply a temporal aspect, a spatial aspect, an ordering, etc. Rather, such terms are merely used as identifiers, names, etc. for features, elements, items, etc. For example, a first channel and a second channel generally correspond to channel A and channel B or two different or two identical channels or the same channel. Additionally, “comprising”, “comprises”, “including”, “includes”, or the like generally means comprising or including, but not limited thereto.\|[0068] Further, the term “in” as used to describe an object with respect to a given direction (e.g., an edge extended in a left-right direction) is intended to denote an orientation that is substantially parallel to the specified direction. In contrast, the term “along” as used to describe an object with respect to a given direction (e.g., an edge extended along a vertical direction) is intended to indicate that a feature or element possesses a common vector component in that direction, even if its overall alignment is not strictly parallel.\|[0069] The foregoing outlines features of several embodiments so that those skilled in the art may better understand the aspects of the present disclosure. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions and/or alternative embodiments exist that employ alternative materials, mixtures, proportions, sizes, etc., do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.	Family Number\|(116414688)\|116414688\|Title\|(US20250333914 A1)\|Carbon capture system and method for synthetic turf fields\|(WO2025222295 A1)\|Carbon capture system and method for synthetic turf fields\|Advantages / Prev. Drawbacks\|(US20250333914 A1)\|Furthermore, it will be appreciated that by placing the rock dust 102 into the subgrade 210, additional opportunity to capture carbon is presented, as soil contains more carbon dioxide then air.\|It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|(WO2025222295 A1)\|It will be appreciated that placement of the rock dust 102 as shown in FIG. 6 may provide additional time for weathering of the rock dust 102, as the incorporation of the rock dust 102 into the first base stone layer 200 and the second base stone layer 202 may hold water for extended periods of time.\|Independent Claims\|(US20250333914 A1)\| (...) rock dust including silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, wherein at least 90 percent of the rock dust has a particle size less than 250 micrometers in diameter; and\| (...) dispersing rock dust over a top portion of turf fibers, wherein the rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|(WO2025222295 A1)\|14. Infill for a synthetic turf system, the infill comprising: rock dust including silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater, wherein at least 90 percent of the rock dust has a particle size less than 250 micrometers in diameter; and organic particles, rubber particles, elastomer (...) \|17. A method of preparing a synthetic turf system, the method comprising: dispersing rock dust over a top portion of turf fibers, wherein the rock dust includes silicate rock, igneous rock, or reactive rock that forms a carbonate or bicarbonate with rainwater traveling through one or more infill layers.\|	Civil engineering\|Environmental technology	E01C-013/02\|E01C-013/08		E01C-013/02\|E01C-013/08	B01D-053/62\|E01C-013/02\|E01C-013/08\|E01H-015/00	B01D-053/62\|E01C-013/02\|E01C-013/08\|E01H-015/00					JP2006219870\|US20110081506\|EP3929246	JP2006219870 32443123 WHO=Examiner SELF=N CAT=Y\|US20110081506 7741571 WHO=Examiner SELF=N CAT=X CAT=Y\|EP3929246 97939753 WHO=Examiner SELF=N CAT=A		US20110081506; JP2006219870; EP3929246\|		PENDING	(US20250333914)\|PENDING\|(WO2025/222295)\|PENDING	ALIVE	(US20250333914)\|ALIVE\|(WO2025/222295)\|ALIVE	(US20250333914)\|LEGAL DETAILS FOR US20250333914\|Actual or expected expiration date=2045-04-23\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-04-23\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19186905\|Application date=2025-04-23\|Standardized application number=2025US-19186905\|Event publication date=2025-04-23\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-04-23\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-04-23\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 58213-00341\|Event publication date=2025-04-23\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 136458\|Event publication date=2025-04-23\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2025-04-23\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-04-23\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-04-29\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-05-22\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-05-28\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2025-06-10\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-06-10\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-10-30\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250333914\|Publication stage code=A1\|Publication date=2025-10-30\|Standardized publication number=US20250333914\|Event publication date=2025-10-30\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2025-11-06\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|(WO2025/222295)\|LEGAL DETAILS FOR WO2025/222295\|Actual or expected expiration date=2027-10-24\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-04-23\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOCA2025/050589\|Application date=2025-04-23\|Standardized application number=2025WO-CA50589\|Event publication date=2025-10-30\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/222295\|Publication stage code=A1\|Publication date=2025-10-30\|Standardized publication number=WO2025222295\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2045-04-23\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP25793131\|Event publication date=2025-12-10\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP	(WO2025/222295)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/222295)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/222295)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/222295)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/222295)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UY, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(US20250333914)\|US\|(WO2025/222295)\|WO; EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcPHl2qs/cUhz3ePXCJGwxO7JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023092496&ekey=2099&xpn=US20250333914&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19186905/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=KfuhNexKo8%252FE99EbR8WxkcRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2025/222295)\|CA\|(US20250333914)\|CA	(WO2025/222295)\|NAME=TARKETT SPORTS CANADA INC. 7445 Cote-de-Liesse Road, Suite 200 Montreal, Québec H4T 1G2 , COUNTRY=CA\|(US20250333914)\|NAME=Tarkett Sports Canada Inc. , CITY=Montreal , COUNTRY=CA	(WO2025/222295)\|CA	(WO2025/222295)\|NAME=YIP, Vincent Suite 2400-745 Thurlow Street Vancouver, British Columbia V6E 0C5 , POSTCODE=V6E 0C5 , COUNTRY=CA	(US20250333914)\|CA; CA; US\|(WO2025/222295)\|CA; CA; US	(US20250333914)\|NAME=Smollett Jason, CITY=Kirkland, COUNTRY=CA \|NAME=Habib Eric, CITY=Pierrefonds, COUNTRY=CA \|NAME=Chisam Christopher, CITY=Granite Bay, STATE=CA , COUNTRY=US\|(WO2025/222295)\|NAME=SMOLLETT, Jason 71 Rondeau Kirkland, Québec H9H4J2, POSTCODE=H9H4J2, COUNTRY=CA \|NAME=HABIB, Eric 4967 Saint Barnabas Pierrefonds, Québec H8Z3B9, POSTCODE=H8Z3B9, COUNTRY=CA \|NAME=CHISAM, Christopher 9792 Swan Lake Drive Granite Bay, California 95746, POSTCODE=95746, COUNTRY=US	(WO2025/222295)\|9\|(US20250333914)\|9	2	2					(US20250333914)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,14,17\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|\|(WO2025/222295)\|Number of Claims: NCL=20\|Extended kind: EXTK=x\|	(US20250333914)\|Provisional Appl: US63/638,100 FDD=2024-04-24 [2024US-63638100]	(US20250333914)\|ENGLISH (ENG)	(US20250333914)\|Patent\|(WO2025222295)\|Patent	Titre: (US20250333914)\|Carbon capture system and method for synthetic turf fields Résumé: (US20250333914)\|A synthetic turf system including a backing, turf fibers extended upward from the backing, and one or more infill layers positioned above the backing, below a top portion of the turf fibers. The one or more infill layers includes rock dust, or the synthetic turf system further includes a layer of the rock dust disposed above or below the one or more infill layers. The rock dust is accessible to rainwater from the top portion of the turf fibers, where the rainwater and the rock dust chemically react with each other, forming a carbonate or a bicarbonate.	18	Abstract	gpt-4o-mini	yes	The article describes a system that uses rock dust in synthetic turf to chemically react with rainwater, forming carbonates or bicarbonates, which aligns with the goal of carbon sequestration.
19	capturing (...) \|(WO2023114474 A2)\|1. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; and capturing CO2 from air using the hydroxide-rich stream (...) \|13. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising salt water and at least one of a mineral and a metal; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; capturing CO2 from (...) \|17. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process comprising electrolysis with an electrolysis unit to produce at least one hydroxide-rich stream; capturing CO2 from air (...) \|(AU2022413289 A1)\|1. A method for capturing and sequestering carbon dioxide (002)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; and capturing 002 from air using the hydroxide-rich stream (...) \|13. A method for capturing and sequestering carbon dioxide (002)	comprising: receiving an input liquid comprising salt water and at least one of a mineral and a metal; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; capturing 002 from (...) \|17. A method for capturing and sequestering carbon dioxide (002)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process comprising electrolysis with an electrolysis unit to produce at least one hydroxide-rich stream; capturing 007 from air (...) \|(CA3241195 A1)\| (...) A method for capturing and sequestering carbon dioxide (002)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; and capturing CO2 from air using the hydroxide-rich stream (...) \|13. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising salt water and at least one of a mineral and a metal; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; capturing CO2 from (...) \|17. A method for capturing and sequestering carbon dioxide (CO2)	comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process comprising electrolysis with an electrolysis unit to produce at least one hydroxide-rich stream; capturing CO	from air (...) \|(KR20240134132 A)\|1. A method for capturing and isolating carbon dioxide (CO2)	the method comprising:receiving an input liquid comprising water and a salt;performing an electrochemical process on the input liquid to produce at least one hydroxide rich stream; and capturing CO2 from (...) \|13. A method for capturing and isolating carbon dioxide (CO2)	comprising:receiving an input liquid comprising salt water and at least one of a mineral and a metal;performing an electrochemical process on the input liquid to produce at least one hydroxide rich stream;capturing (...) \|17. A method for capturing and isolating carbon dioxide (CO2)	the method comprising:receiving an input liquid comprising water and a salt;performing an electrochemical process comprising electrolysis with an electrolysis unit to produce at least one hydroxide rich stream;capturing (...) \|(JP2024545883 A)\|1. A method for capturing and isolating carbon dioxide (CO2)	the method comprising the steps of: receiving a feed liquid containing water and a salt; subjecting the feed liquid to an electrochemical process to produce at least one hydroxide-rich stream; and trapping CO2 (...) \|13. A method for capturing and isolating carbon dioxide (CO2)	which comprises the steps of: receiving a feed liquid containing salt water	a mineral and/or a metal; producing at least one hydroxide-rich stream by subjecting the feed liquid to an electrochemical process; capturing (...) \|17. A method for capturing and isolating carbon dioxide (CO2)	which comprises the steps of: receiving a charged liquid containing water and a salt; producing at least one hydroxide-rich stream by conducting an electrochemical process including electrolysis with an electrolysis (...) \|"	Chemical engineering\|Environmental technology\|Materials, metallurgy\|Surface technology, coating	B01D-053/62\|B01D-053/78\|B01D-053/79\|B01D-053/96/5\|B01D-2251/604\|B01D-2251/606\|B01D-2257/504\|B01D-2258/06\|C01B-032/60\|C22B-007/00\|C22B-026/12\|C25B-001/04\|C25B-001/26\|C25B-001/34\|C25B-015/08\|Y02C-020/40\|Y02P-020/151		B01D-053/62\|B01D-053/78\|B01D-053/79\|B01D-053/96/5\|B01D-2251/604\|B01D-2251/606\|B01D-2257/504\|B01D-2258/06\|C01B-032/60\|C22B-007/00\|C22B-026/12\|C25B-001/04\|C25B-001/26\|C25B-001/34\|C25B-015/08\|Y02C-020/40\|Y02P-020/151	B01D-053/62\|B01D-053/78\|B01D-053/79\|B01D-053/96\|B01D-061/02\|B01D-061/44\|B01D-061/46\|C01B-032/60\|C01F-011/18\|C02F-001/42\|C02F-001/461\|C02F-001/469\|C22B-007/00\|C22B-026/12\|C25B-001/34	B01D-053/62\|B01D-053/78\|B01D-053/79\|B01D-053/96\|B01D-061/02\|B01D-061/44\|B01D-061/46\|C01B-032/60\|C01F-011/18\|C02F-001/42\|C02F-001/461\|C02F-001/469\|C22B-007/00\|C22B-026/12\|C25B-001/34			WO202585683\|WO2025116282\|WO2025222207\|WO2025230893\|WO2025166109\|WO202590603\|WO2025184747;WO2025184747\|WO202477053\|WO202622817\|WO2025155846\|WO2025155543\|WO202596690\|WO2025128708\|KR102836116\|US12378847\|US12435601\|US12134574\|US12172910\|US12359323\|US12359323\|US12359323\|US12258754	WO202585683 114153000 WHO=Examiner SELF=Y CAT=Y CAT=A\|WO2025116282 114785158 WHO=Examiner SELF=N CAT=Y\|WO2025222207 116330603 WHO=Examiner SELF=Y CAT=X CAT=Y\|WO2025230893 116414470 WHO=Examiner SELF=N CAT=X CAT=I\|WO2025166109 115547616 WHO=Examiner SELF=N CAT=X CAT=I\|WO202590603 114240222 WHO=Examiner SELF=N CAT=X CAT=I\|WO2025184747 115937670 WHO=Examiner SELF=N CAT=X\|WO202477053 109306669 WHO=Examiner SELF=Y CAT=E CAT=X\|WO202622817 117592933 WHO=Examiner SELF=N CAT=A\|WO2025155846 115384923 WHO=Examiner SELF=N CAT=A\|WO2025155543 115384923 WHO=Examiner SELF=N CAT=A\|WO202596690 114470421 WHO=Examiner SELF=N CAT=A\|WO2025128708 114878955 WHO=Applicant SELF=N\|KR102836116 115308820 WHO=Applicant SELF=N\|US12378847 114878954 WHO=Applicant SELF=N\|US12435601 114878955 WHO=Applicant SELF=N\|US12134574 111586813 WHO=Examiner SELF=N\|US12172910 111586813 WHO=Applicant SELF=N\|US12359323 104556615 WHO=Applicant SELF=N\|US12359323 104556615 WHO=Applicant SELF=N\|US12359323 104556615 WHO=Applicant SELF=N\|US12258754 92775698 WHO=Examiner SELF=N	KR20160034635\|KR20160034635\|US20140301922\|US20140301922\|US20120312697\|US20110135551\|US20110135551\|US20100150802\|US20100150802\|US3712025\|US20210001270\|US20210001270\|FR2998811\|WO2020163513\|WO201181254\|US20200291901\|US20110203939\|US20110203939\|US20080245672\|US20210001270\|US20110203939\|US20100150802\|US20210001270\|US20200370001\|JP2019194154\|EP3765174\|KR102032948\|TWI708740\|US20180036685\|EP3074349\|KR20160034635\|US20140301922\|US9784140\|KR20140042394\|US9689309\|JP3174102U\|US9422176\|JP5932771\|US20110135551\|US20110203939\|US8551221\|US8470275\|WO2010104751\|US20100150802\|US20110094230\|US20110226010\|US20060051274\|EP2070583\|US7637093\|WO200029326\|WO200010691	KR20160034635 72551329 WHO=Examiner SELF=N CAT=Y\|KR20160034635 72551329 WHO=Examiner SELF=N CAT=Y\|US20140301922 66134158 WHO=Examiner SELF=N CAT=Y\|US20140301922 66134158 WHO=Examiner SELF=N CAT=Y\|US20120312697 73733989 WHO=Examiner SELF=N 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1682257 WHO=Applicant SELF=N\|WO200029326 1279369 WHO=Applicant SELF=N\|WO200010691 1466053 WHO=Applicant SELF=N		\|US20210001270; US20100150802; KR20160034635; US20140301922; US20110135551; US20110203939\|US20210001270; US20100150802; KR20160034635; US20140301922; US20110135551; US20110203939; WO201181254; FR2998811; US20120312697; US3712025; WO2020163513; US20080245672; US20200291901\|\|\|\|\|US20210001270; US20110203939; US20100150802; US7637093; US8470275; US8551221; US9422176; US9689309; US9784140; US20060051274; US20100150802; US20110094230; US20110135551; US20110203939; US20110226010; US20140301922; US20180036685; US20200370001; US20210001270; EP2070583; EP3074349; EP3765174; JP3174102U; JP5932771; JP2019194154; KR20140042394; KR20160034635; KR102032948; TWI708740; WO2010104751; WO200010691; WO200029326	\|(US12030016)\|Applicant references\|-Holmes, G. J., “A carbon dioxide absorpiton performance evaluation for capture from ambient air”, 2010, Publisher: University of Calgary, Published in: Calgary.\|-Baciocchi et al., “Process design and energy requirements for the capture of carbon dioxide from air”, 2006.\|-Caldeira et al., “Accelerating carbonate dissolution to sequester carbon dioxide in the ocean: Geochemical implications”, 2000.\|-Dong et al., “Direct Air Capture via Natural Draft Dry Cooling Tower”, 2021.\|-Du et al., “Treatment of Brackish Water RO Brine via Bipolar Membrane Electrodialysis”, 2021.\|-Gmar et al., “Recent advances on electrodialysis for the recovery of lithium from primary and secondary resources”, 2019.\|-Hanein et al., “Decarbonisation of calcium carbonate at atmospheric temperatures and pressures, with simultaneous CO2 capture, through production of sodium carbonate”, Energy & Environmental Science, 2021, p. 65956604, vol. 14, No. 6595.\|-Herrero-Gonzalez et al., “Highly concentrated HCI and NaOH from brines using electrodialysis with bipolar membranes”, 2020.\|-Holmes et al., “Outdoor prototype results for direct atmospheric capture of carbon dioxide”, 2013.\|-House et al., “Economic and energetic analysis of capturing CO2 from ambient air”, 2011.\|-Jiang et al., “Production of Lithium Hydroxide from Lake Brines through ElectroElectrodialysis with Bipolar Membranes (EEDBM)”, 2014.\|-Keith et al., “A Process for Capturing CO2 from the Atmosphere”, 2018, Publisher: Elsevier.\|-Kim, D.H., “A review of desalting process techniques and economic analysis of the recovery of salts from retentates”, 2011.\|-Kuldeep et al., “Bipolar Membrane Electrodialysis for Sulfate Recycling in the Metallurgical Industries”, 2021.\|-Maharloo et al., “Process intensification and environmental consideration of sodium bicarbonate production in an industrial soda ash bubble column reactor by CO2 recycling”, 2017.\|-Mahmoudkhani et al., “Low-energy sodium hydroxide recovery for CO2 capture from atmospheric airThermodynamic analysis”, 2009.\|-Newsom, Gavin, “Selective Recovery of Lithium from Geothermal Brines”, 2020.\|-Pohorecki et al., “Kinetics of Reaction Between Carbon Dioxide and Hydroxyl Ions in Aqueous Electrolyte Solutions”, 1988.\|-Renforth et al., “Assessing ocean alkalinity for carbon sequestration”, 2017.\|-Digdaya et al., “A direct coupled electrochemical system for capture and conversion of CO2 from oceanwater”, Nature Communications, 2020.\|-Du et al., “Supporting Information for Sodium Hydroxide Production from Seawater Desalination Brine: Process Design and Energy efficiency”, Environmental Science & Technology, 2018, Published in: US.\|-Holmes et al., “An air-liquid contactor for large-scale capture of CO2 from air”, Philosophical Transactions of The Royal Society, 2012, pp. 4380-4403, vol. 370.\|-Sanz-Perez et al., “Direct Capture of CO2 from Ambient Air”, Chemical Reviews, 2016, pp. 11840-11876, vol. 116.\|-Smith, Stephen V., “Parsing the Oceanic Calcium Carbonate Cycle: A Net Atmospheric Carbon Dioxide Source, or a Sink?”, 2013.\|-Renforth et al., “Engineering challenges of ocean liming”, 2013.\|-Ruiz et al., “Sustainable and Negative Carbon Footprint Solid-Based NaOH Technology for CO2 Capture”, 2020.\|-Saberi et al., “Precipitation kinetics of sodium bicarbonate in an industrial bubble column crystallizer”, 2009.\|-Sen et al., “Hydroxide Based Integrated CO2 Capture from Air and Conversion to Methanol”, 2020.\|-Shaikh et al., “Scale-up of Bubble Column Reactors: A Review of Current State-of-the-Art”, 2013.\|-Shim et al., “Experimental study on capture of carbon dioxide and production of sodium bicarbonate from sodium hydroxide”, 2016.\|-Socolow et al., “Direct Air Capture of CO2 with Chemicals”, 2011.\|-Song et al., “Separation of sodium hydroxide from post-carbonation brines by bipolar membrane electrodialysis (BMED)”, 2021.\|-Sujoto et al., “Lithium recovery from synthetic geothermal brine using electrodialysis method”, 2021.\|-Telzhensky et al., “Selective separation of seawater Mg2+ ions for use in downstream water treatment processes”, 2011.\|-Wang et al., “Packing characterization for post combustion CO2 capture: mass transfer model development”, 2014.\|-Warren, I., “Techno-Economic Analysis of Lithium Extraction from Geothermal Brines”, 2021.\|-Wylock et al., “Compartmental Modeling of an Industrial Column”, 2009.\|-Xue et al., “Total alkalinity minus dissolved inorganic carbon as a proxy for deciphering ocean acidification mechanisms”, 2020.\|-Zeman et al., “Production of carbon negative precipitated calcium carbonate from waste concreate”, 2016.\|-Du et al., “Sodium hydroxide production from seawater desalination brine: process design and energy efficiency”, 2018.\|-Amaral et al., “Modelling gas-liquid mass transfer in wastewater treatment: when current knowledge needs to encounter engineering practice and vice versa.” Water Science & Technology \| 80.4 \| 2019.\|-Andersen, C. Brannon., “Understanding Carbonate Equilibria by Measuring Alkalinity in Experimental and Natural Systems.” Journal of Geoscience Education, v. 50, n. 4, Sep. 2002, p. 389-403.\|-Ayirala, S.C. and Yousef, A.A., “A Critical Review of Alternative Desalination Technologies for Smart Waterflooding.” Oil and Gas Facilities, Oct. 2016.\|-Ayoub, George M., Ramez M. Zayyat, and Mahmoud Al-Hindi., “Precipitation Softening: A Pretreatment Process for Seawater Desalination.” Environmental Science and Pollution Research 21, No. 4 (Feb. 1, 2014): 2876-87. https://doi.org/10.1007/s11356-013-2237-1.\|-Dahmani et al., “Removal of Ca(II) and Mg(II) hardness by ion exchange resins and soda ash for seawater pretreatment to reduce scale formation in evaporators multi-stage flash desalination.” Desalination and Water Treatment 221 (2021) 23-30.\|-Kiepe et al. “Experimental Determination and Prediction of Gas Solubility Data for CO2 + H2O Mixtures Containing NaCI or KCI at Temperatures between 313 and 393 K and Pressures up to 10 MPa.” Ind. Eng. Chem. Res. 2002, 41, 4393-4398.\|-Kucka et al., “Kinetics of the Gas-Liquid Reaction between Carbon Dioxide and Hydroxide Ions.” Ind. Eng. Chem. Res. 2002, 41, 5952-5957.\|-Macedonio, F., and E. Drioli. “4.09—Membrane Systems for Seawater and Brackish Water Desalination.” In Comprehensive Membrane Science and Engineering, edited by Enrico Drioli and Lidietta Giorno, 241-57. Oxford: Elsevier, 2010. https://doi.org/10.1016/B978-0-08-093250-7.00056-6.\|-Mahmoudkhani et al., “Low energy packed tower and caustic recovery for direct capture of CO2 from air.” Energy Procedia 1 (2009) 1535-1542.\|-“Mazzotti et al., “Direct air capture of CO2 with chemicals: optimization of a two-loop hydroxide carbonate system usinga countercurrent air-liquid contactor.” Climatic Change (2013) 118:119-135”.\|-Nelson et al., “Remineralization and Stabilization of Desalinated Water.”, 2021, https://www.intechopen.com/chapters/78990.\|-Pinsent et al., “The Kinetics of Combination of Carbon Dioxide With Hydroxide Ions.” Dept. of Colloid Science, University of Cambridge, 1956, 1512-1520.\|-Suhalim et al., “A. Rejection Mechanism of lonic Solute Removal by Nanofiltration Membranes: An Overview.”, Nanomaterials Dec. 2022, 437. https://doi.org/10.3390/nano12030437.\|-Thuy et al., “Removal of Hydrogen Sulfide in Synthesized Air by Chemical Absorption in a Packed Column.” Tap chí Khoa hc Công nghe và Thuc pham 18 (2) (2019) 3-11.\|-U.S. Environmental Protection Agency—Office of Water Program Operations, “Physical-Chemical Treatment Technology—Training Manual”, 1977.\|-Voutchkov, Nikolay. “Re-mineralization of Desalinated Water.” 2011.\|\|\|\|\|\|\|	GRANTED	(EP4448148)\|PENDING\|(US12030016)\|GRANTED\|(US20240238721)\|PENDING\|(WO2023/114474)\|LAPSED\|(JP2024545883)\|PENDING\|(KR10-2024-0134132)\|PENDING\|(AU2022413289)\|PENDING\|(CA3241195)\|PENDING	ALIVE	(EP4448148)\|ALIVE\|(US12030016)\|ALIVE\|(US20240238721)\|ALIVE\|(WO2023/114474)\|DEAD\|(JP2024545883)\|ALIVE\|(KR10-2024-0134132)\|ALIVE\|(AU2022413289)\|ALIVE\|(CA3241195)\|ALIVE	(EP4448148)\|LEGAL DETAILS FOR EP4448148\|Actual or expected 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state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=KR Corresponding appl: KR10-2024-7023462\|Application date in the designated or member state=2022-12-16\|Application number in the designated or member state=2024KR-7023462\|Corresponding cc:\|Designated or member state=KR Corresponding pat: KR10-2024-0134132\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2024-09-06\|Publication number in the designated or member state=KR20240134132\|Event publication date=2024-07-12\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=KR\|MEMBER STATE LEGAL DETAILS FOR NZ\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=NZ Corresponding appl: NZ808523\|Event publication date=2024-02-22\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into 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date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-12-16\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2022413289\|Application date=2022-12-16\|Standardized application number=2022AU-0413289\|Event publication date=2024-03-07\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2022413289\|Publication stage code=A1\|Publication date=2024-03-07\|Standardized publication number=AU2022413289\|(CA3241195)\|LEGAL DETAILS FOR CA3241195\|Actual or expected expiration date=2042-12-16\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-12-16\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA3241195\|Application date=2022-12-16\|Standardized application number=2022CA-3241195\|Event publication date=2023-06-22\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA3241195\|Publication stage code=A1\|Publication date=2023-06-22\|Standardized publication number=CA3241195	(EP4448148)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2023/114474)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2023/114474)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2023/114474)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2023/114474)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2023/114474)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, 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NZ\|(JP2024545883)\|JP\|(KR10-2024-0134132)\|KR\|(AU2022413289)\|AU\|(CA3241195)\|CA	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=ECLncZT9nTVX7AnVeY5F63mXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022061326&ekey=2149&xpn=EP4448148&kind=A4	https://register.epo.org/application?number=EP22908488	https://permalink.orbit.com/RenderStaticFirstPage?XPN=atIwPveYDDMbWDK85JFymXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(US20240238721)\|US\|(WO2023/114474)\|US\|(WO2023/114474)\|US\|(US12030016)\|US\|(US20230191322)\|US	(US20240238721)\|NAME=Capture6 Corp. , CITY=Berkeley , STATE=CA , COUNTRY=US\|(WO2023/114474)\|NAME=CAPTURE6 CORP 1340 Josephine St Berkeley, California 94703 , COUNTRY=US\|(WO2023/114474)\|NAME=CAPTURE6 CORP 1340 Josephine St Berkeley, California 94703 , COUNTRY=US\|(US12030016)\|NAME=Capture6 Corp , CITY=Berkeley , STATE=CA , COUNTRY=US , ATYP=US Company\|(US20230191322)\|NAME=Capture6 Corp , CITY=Berkeley , STATE=CA , COUNTRY=US	(EP4448148)\|GB\|\|(WO2023/114474)\|US\|(WO2023/114474)\|US\|\|\|(AU2022413289)\|NZ\|(CA3241195)\|CA	(EP4448148)\|NAME=Dentons UK and Middle East LLP One Fleet Place , CITY=London EC4M 7WS , COUNTRY=GB , REG=101672946\|(US12030016)\|NAME=DENTONS DAVIS BROWN NAME=Warner-Blankenship Matthew\|(WO2023/114474)\|NAME=WARNER-BLANKENSHIP, Matthew 215 10th Street Suite 1300 Des Moines, Iowa 50309 , POSTCODE=50309 , COUNTRY=US\|(WO2023/114474)\|NAME=WARNER-BLANKENSHIP, Matthew 215 10th Street Suite 1300 Des Moines, Iowa 50309 , POSTCODE=50309 , COUNTRY=US\|(JP2024545883)\|NAME=YAMAMOTO Osamu , REG=100118902NAME=MIYAMAE,Toru , REG=100106208NAME=MATSUO JUNICHI , REG=100196508NAME=YOKOTA KOICHI , REG=100196597\|(KR10-2024-0134132)\|NAME=KIM, TAE HONG NAME=KIM, JIN HOI\|(AU2022413289)\|NAME=Dentons Patent Attorneys Australasia Limited 18 Viaduct Harbour Avenue , CITY=Auckland CBD , POSTCODE=1142 , COUNTRY=NZ\|(CA3241195)\|NAME=BORDEN LADNER GERVAIS LLP , COUNTRY=CA	\|(EP4448148)\|US; NZ; US; US\|(US12030016)\|US; US; NZ; US\|(US20230191322)\|NZ; US; US; US\|(US20240238721)\|US; NZ; US; US\|(WO2023/114474)\|US; NZ; US; US\|(WO2023/114474)\|US; NZ; US; US\|\|\|\|(CA3241195)\|US; NZ; US; US	(EP4448148)\|NAME=COHEN-COLE, Ethan\|NAME=SHORS, Luke\|NAME=SURANA, Rahul\|NAME=LANDAU, Zeph\|(EP4448148)\|NAME=COHEN-COLE, Ethan, CITY=Berkeley, California 94703, COUNTRY=US \|NAME=SHORS, Luke, CITY=Rotorua,, COUNTRY=NZ \|NAME=SURANA, Rahul, CITY=Fremont, CA 94539, COUNTRY=US \|NAME=LANDAU, Zeph, CITY=Berkeley, California 94702, COUNTRY=US\|(US12030016)\|NAME=Cohen-Cole Ethan, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Surana Rahul, CITY=Fremont, STATE=CA , COUNTRY=US \|NAME=Shors Luke, CITY=Rotorua, COUNTRY=NZ \|NAME=Landau Zeph, CITY=Berkeley, STATE=CA , COUNTRY=US\|(US20230191322)\|NAME=Shors Luke, CITY=Rotorua, COUNTRY=NZ \|NAME=Landau Zeph, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Cohen-Cole Ethan, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Surana Rahul, CITY=Fremont, STATE=CA , COUNTRY=US\|(US20240238721)\|NAME=COHEN-COLE ETHAN, CITY=Berkeley, STATE=CA , COUNTRY=US \|NAME=Shors Luke, CITY=Rotorua, COUNTRY=NZ \|NAME=Surana Rahul, CITY=Fremont, STATE=CA , COUNTRY=US \|NAME=Landau Zeph, CITY=Berkeley, STATE=CA , COUNTRY=US\|(WO2023/114474)\|NAME=COHEN-COLE, Ethan 1340 Josephine St Berkeley, California 94703, POSTCODE=94703, COUNTRY=US \|NAME=SHORS, Luke 128 Iles Rd Rotorua, COUNTRY=NZ \|NAME=SURANA, Rahul 47066 Palo Amarillo Dr. Fremont, CA 94539, POSTCODE=94539, COUNTRY=US \|NAME=LANDAU, Zeph 1346 Curtis Street Berkeley, California 94702, POSTCODE=94702, COUNTRY=US\|(WO2023/114474)\|NAME=COHEN-COLE, Ethan 1340 Josephine St Berkeley, California 94703, POSTCODE=94703, COUNTRY=US \|NAME=SHORS, Luke 128 Iles Rd Rotorua, COUNTRY=NZ \|NAME=SURANA, Rahul 47066 Palo Amarillo Dr. Fremont, CA 94539, POSTCODE=94539, COUNTRY=US \|NAME=LANDAU, Zeph 1346 Curtis Street Berkeley, California 94702, POSTCODE=94702, COUNTRY=US\|(JP2024545883)\|NAME=Cohen Cole, Ethan\|NAME=Shores, Luke\|NAME=Surana, Rahul\|NAME=Zeff Landau\|(KR10-2024-0134132)\|NAME=COHEN COLE ETHAN\|NAME=SHORS LUKE\|NAME=SURANA RAHUL\|NAME=LANDAU ZEPH\|(AU2022413289)\|NAME=COHEN-COLE, Ethan\|NAME=SHORS, Luke\|NAME=SURANA, Rahul\|NAME=LANDAU, Zeph\|(CA3241195)\|NAME=COHEN-COLE, ETHAN, COUNTRY=US \|NAME=SHORS, LUKE, COUNTRY=NZ \|NAME=SURANA, RAHUL, COUNTRY=US \|NAME=LANDAU, ZEPH, COUNTRY=US	(US20240238721)\|50\|\|(JP2024545883)\|10\|(KR10-2024-0134132)\|50\|(AU2022413289)\|47\|(CA3241195)\|50\|(US12030016)\|50	8	8				(EP4448148)\|WO2023/114474\|(JP2024545883)\|WO2023/114474\|(KR10-2024-0134132)\|WO2023/114474\|(AU2022413289)\|WO2023/114474\|(CA3241195)\|WO2023/114474		(US12030016)\|Number of Claims: NCL=7\|Number of Drawings: NDR=50\|Number of Figures: NFG=50\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=0\|Primary examiner: Patel Smita S\|Art Unit.: ART =1732\|\|(US20230191322)\|Number of Claims: NCL=20\|Number of Drawings: NDR=50\|Number of Figures: NFG=50\|Independent Claim Number: ICL=1,13,17\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|Primary examiner: Patel Smita S\|Art Unit.: ART =1732\|\|(US20240238721)\|Number of Claims: NCL=20\|Number of Drawings: NDR=50\|Number of Figures: NFG=50\|Exemplary Claim Number: ECL=21\|\|(WO2023/114474)\|Number of Claims: NCL=20\|Extended kind: EXTK=z\|\|(JP2024545883)\|Number of Claims: NCL=20\|Request for examination: REQEXA=false\|\|(KR10-2024-0134132)\|Number of Claims: NCL=20\|\|(AU2022413289)\|Number of Claims: NCL=20\|\|(CA3241195)\|Number of Claims: NCL=20\|	(US12030016)\|Provisional Appl: US63/290,467 FDD=2021-12-16 [2021US-63290467]\|Provisional Appl: US63/341,883 FDD=2022-05-13 [2022US-63341883]\|Provisional Appl: US63/355,368 FDD=2022-06-24 [2022US-63355368]\|Provisional Appl: US63/389,095 FDD=2022-07-14 [2022US-63389095]\|Provisional Appl: US63/413,021 FDD=2022-10-04 [2022US-63413021]\|Previous publication: US20230191322 A1 2023-06-22 [US20230191322]\|(US20240238721)\|Continuation of: US18/082,903 FDD=2022-12-16 [2022US-18082903]\|Provisional Appl: US63/413,021 FDD=2022-10-04 [2022US-63413021]\|Provisional Appl: US63/389,095 FDD=2022-07-14 [2022US-63389095]\|Provisional Appl: US63/355,368 FDD=2022-06-24 [2022US-63355368]\|Provisional Appl: US63/341,883 FDD=2022-05-13 [2022US-63341883]\|Provisional Appl: US63/290,467 FDD=2021-12-16 [2021US-63290467]	(EP4448148)\|ENGLISH (ENG)	CC=KR ORG=QUESTEL			(EP4448148)\|Patent\|(JP2024545883)\|Patent\|(EP4448148)\|Patent\|(KR20240134132)\|Patent\|(US20240238721)\|Patent\|(US12030016)\|Patent\|(AU2022413289)\|Patent\|(WO2023114474)\|Patent\|(CA3241195)\|Patent\|(US20230191322)\|Patent\|(WO2023114474)\|Patent				Titre: from air (...) \|(KR20240134132 A)\|1. A method for capturing and isolating carbon dioxide (CO2) Résumé: the method comprising:receiving an input liquid comprising water and a salt;performing an electrochemical process on the input liquid to produce at least one hydroxide rich stream; and capturing CO2 from (...) \|13. A method for capturing and isolating carbon dioxide (CO2)	17	Abstract	gpt-4o-mini	no	The article focuses on capturing and isolating CO2 through an electrochemical process, which does not involve the accelerated weathering of minerals or the specific methods related to enhanced weathering.
20	CN202511559558	CN202511559558	CN121253236	117274553	CN121253236 A 2026-01-02 [CN121253236]	2025-10-29	2025-10-29	2026-01-02		(CN121253236)\|2045-10-29	(CN121253236)\|Buried soil water collecting system	(CN121253236)\|The invention provides a buried soil water collection system, and belongs to the technical field of rock weathering carbon sequestration and salinized soil transformation and governance, a porous ceramic tube is buried in soil, a porous water absorption material and an extrusion assembly for extruding the porous water absorption material are arranged in the porous ceramic tube, and soil water adsorbed in the soil is absorbed by the porous ceramic tube under the capillary action, so that the soil water is absorbed by the porous ceramic tube; the soil water is adsorbed and transmitted to the porous water absorption material through the microporous structure of the porous ceramic tube, and the porous water absorption material can continuously adsorb and store the soil water. When the water storage amount in the porous water absorption material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorption material, so that the soil water stored in the porous water absorption material is extruded out, and the extruded soil water is drained to the water storage container through the water outlet holes in the porous ceramic pipe and the liquid guide pipe, so that the soil water is centrally stored in the water storage container. Therefore, the real soil water sample can be stably and efficiently collected for a long time under the field condition that the in-situ structure and the moisture dynamic state of the soil are not damaged.	LANZHOU UNIVERSITY\|MICROCARBON LOW CARBON TECHNOLOGY	(CN121253236)\|LANZHOU UNIVERSITY ([CN])\|Microcarbon (Guangzhou) Low Carbon Technology Co., Ltd.	ZHANG JIETANG\|LI XINGYUAN\|GOU XIAOHUA	(CN121253236)\|ZHANG JIETANG\|LI XINGYUAN\|GOU XIAOHUA	(CN121253236)\|HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP)\|Reg. Nb: 41028	(CN121253236)\|Compared with the prior art, the buried soil water collecting system provided by the embodiment of the invention has the advantages that the porous ceramic tube 21 with the wall having the micropore structure is buried in soil, the porous water absorbing material 22 capable of absorbing and storing soil water and the extrusion component 3 capable of extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22 are arranged in the porous ceramic tube 21, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic tube 21 under the capillary action, and is absorbed and transmitted to the porous water absorbing material 22 through the micropore structure of the porous ceramic tube 21, so that the porous water absorbing material 22 can continuously absorb and store the soil water.\|It will be appreciated that in some embodiments, the filter layer comprises at least one layer of non-woven fabric, because the non-woven fabric has the advantages of being flexible, light in weight, non-toxic, easy to decompose, low in cost, and the like, the porous ceramic tube 21 can be effectively wrapped by the non-woven fabric as the filter layer, so that the pollution to soil water is avoided, the pollution to soil is low, and meanwhile, the cost of the buried soil water collecting system can be effectively controlled.\|Therefore, in the research and product development of enhancing silicate mineral weathering for improvement of salty soil and carbon fixation, there is a need for a technical scheme capable of efficiently collecting real soil water samples under the condition of not damaging the in-situ structure and the moisture dynamics of soil so as to obtain reliable weathering reaction, salt replacement and carbon fixation process data and promote the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|2) The salt migration data is inaccurate, namely, the surface water sample is often influenced by evaporation, precipitation and surface pollution, and the real migration state of the salt with different depths of the section is difficult to reflect;\|Based on the above problems existing in the prior art, an object of the embodiments of the present invention is to provide a buried soil water collection system capable of efficiently collecting real soil water samples under the condition that the in-situ structure and the moisture dynamics of the soil are not damaged, so as to solve the technical problems in the prior art that soil water samples of different soil layers cannot be collected stably and in situ for a long time under the field condition, and chemical composition and hydraulic characteristics of the collected liquid are difficult to be ensured to be consistent with the soil environment.\|	(CN121253236)\|1. A buried soil water collection system, comprising: A fixed bracket; The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.\|	(CN121253236)\|The invention provides a buried soil water collecting system, which belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction and treatment, wherein a porous ceramic tube is buried in soil, a porous water absorbing material and an extrusion component for extruding the porous water absorbing material are arranged in the porous ceramic tube, under the capillary action, the soil water adsorbed in the soil is adsorbed and transferred to the porous water absorbing material through the micropore structure of the porous ceramic tube, and the porous water absorbing material can continuously adsorb and store the soil water.\|The invention provides a buried soil water collecting system, which can collect soil water samples of different soil layers for a long time, stably and in situ under field conditions, and ensure that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for the mechanism research, the effect evaluation and the product optimization of the multifunctional silicate mineral conditioner in the application of improving and fixing the carbon of the saline soil.\|	(CN121253236)\|POROUS CERAMIC TUBE(100,106)\|SOIL WATER COLLECTION(100,35)\|BURIED SOIL WATER COLLECTION(100,9)\|SOIL MOISTURE DYNAMICS(62,2)\|SALINE SOIL RECONSTRUCTION(60,1)\|NONWOVEN FABRIC(55,6)\|EXPERIMENTAL SIMULATION AUTHENTICITY(52,1)\|BURIED SOIL WATER COLLECTING(51,19)\|MOISTURE DYNAMICS(44,2)\|POROUS WATER(40,47)\|ENHANCING SILICATE MINERAL WEATHERING(39,1)\|RESEARCH SCIENTIFICITY(37,1)\|MULTIFUNCTIONAL SILICATE MINERAL CONDITIONER(33,4)\|EXTRUDING POROUS WATER(32,4)\|SALINE SOIL CARBON(31,1)\|SIMULATION EXPERIMENT(31,1)\|DRIVING ROD(30,31)\|BURYING SOIL(30,2)\|GROUND(29,28)\|EXTRUSION COMPONENT(29,11)\|SOIL SALINITY(29,1)\|PULL ROPE(28,6)\|RELIABLE WEATHERING REACTION(28,1)\|REAL MIGRATION(27,1)\|SOIL ENVIRONMENT(26,4)\|EXTRUDE POROUS WATER(24,7)\|CONTAMINATION(24,2)\|MICROPORE(23,5)\|LIQUID COLLECTION(22,8)\|SOIL WATER(21,76)\|MICROPORE STRUCTURE(21,6)\|GROUND LAYER(21,4)\|MINERAL CONDITIONING AGENT DEVELOPMENT(21,1)\|SILICATE MINERAL CONDITIONER(20,4)\|DRIVING EXTRUSION(20,3)\|MINERAL CONDITIONING AGENT(20,1)\|SLIDING HOLE(19,24)\|PUSH PULL ROD(19,22)\|DYNAMIC MOISTURE(19,1)\|FILTER LAYER(18,15)\|SALT MIGRATION DATA(18,1)\|REAL SOIL WATER SAMPLE(17,5)\|TUBE SECTION(16,24)\|MICROPOROUS STRUCTURE(16,10)\|TUBE WALL(16,6)\|BLOCK SEDIMENT(16,2)\|CAPILLARY ACTION(15,11)\|SOIL WATER ADSORBING MEMBER(15,3)\|OUTLET HOLE(15,2)\|PRECIPITATION(15,1)\|SALTY SOIL(15,1)\|COLUMNAR SPONGE END(14,11)\|CARBON FIXATION(14,9)\|SOIL WATER SAMPLE(14,5)\|SLIDING MEMBER(14,2)\|WATER OUTLET(13,15)\|FIXED BRACKET(13,13)\|SOIL WATER ADSORPTION COMPONENT(13,10)\|POROUS WATER COMPRESSION RATIO(12,5)\|COLUMNAR SPONGE DIRECTION(12,3)\|MECHANISM RESEARCH(12,3)\|POROUS WATER ABSORPTION(12,2)\|CERAMIC TUBE(12,1)\|EFFECT EVALUATION(12,1)\|PUSH PULL TUBE GLASS CERAMIC(12,1)\|PRESSING PIECE(11,16)\|ROCK(11,2)\|SLIDING ROD DRIVING(11,2)\|WATER STORAGE CONTAINER(10,16)\|ELASTIC MEMBER(10,7)\|PRESSING MEMBER DRIVING(10,1)\|WATERTIGHT COMPACT STRUCTURE(10,1)\|SOIL WATER EXTRUSION(9,5)\|ACCURATE EXPERIMENTAL DATA(9,3)\|SYMMETRICAL AXIS(9,3)\|CONNECTING ROD(8,16)\|PISTON ROD(8,10)\|COIL SPRING(8,9)\|POROUS STRUCTURE(8,9)\|REPEATABLE EXPERIMENTAL DATA SUPPORT(8,3)\|SURFACE CONTAMINATION(8,1)\|FIXED SUPPORT(7,8)\|LIQUID GUIDE TUBE(7,8)\|COMPRESSION RATIO(7,7)\|POROUS WATER POROUS STRUCTURE(7,6)\|CHEMICAL COMPOSITION(7,4)\|POROUS WATER ABSORPTION MATERIAL(7,4)\|POROUS CERAMIC PIPE(7,3)\|OUTER PERIPHERAL(6,6)\|SLIDING GROOVE(6,6)\|PISTON OUTER CIRCUMFERENTIAL SURFACE(6,3)\|PRODUCT OPTIMIZATION(6,3)\|EXTRUSION SUBASSEMBLY(6,2)\|MINERAL DISSOLUTION REALITY(6,1)\|PRODUCT DEVELOPMENT(6,1)\|SALINE SOIL RECLAMATION(6,1)\|PIPE SECTION(5,17)\|PULLEY BLOCK(5,8)\|WATER ABSORPTION MATERIAL(5,4)\|COLUMN SPONGE(5,3)\|PULLEY BRACKET(5,2)\|CARBON FIXATION PROCESS DATA(5,1)\|CHINESE SALINE ALKALI SOIL(5,1)\|NONWOVEN FABRICS(5,1)\|POTASSIUM MICROELEMENT(5,1)\|PROCESS DATA(5,1)\|SALINE ALKALI BARREN LAND(5,1)\|WATER STORAGE(4,22)\|OPEN END(4,10)\|FIELD CONDITION(4,4)\|MOISTURE DYNAMIC(4,2)\|SALINIZED SOIL IMPROVEMENT(4,2)\|UNCOMPRESSED(4,2)\|AIRTIGHT COMPACT(4,1)\|ECOLOGICAL SAFETY(4,1)\|ERODE ELASTIC PIECE(4,1)\|EXTENSIVE UTILIZATION(4,1)\|WATERPROOF SEALING(4,1)\|WEATHERING EXPERIMENT(4,1)\|OUTER SIDE(3,7)\|PIPE WALL(3,6)\|MOVEABLE PULLEY(3,5)\|CYLINDRICAL SPRING(3,2)\|ELASTICITY(3,2)\|INNER SIDEWALL(3,2)\|SEALING PERFORMANCE ENHANCEMENT(3,2)\|SLIDING SHAFT(3,2)\|SLIDING SLOT(3,2)\|AIRTIGHT SEALING FILM(3,1)\|ATMOSPHERIC CO2 FIXATION(3,1)\|BLOCKING SEDIMENT(3,1)\|ELASTIC BUFFERING ACTION(3,1)\|ENHANCING SILICATE MINERAL(3,1)\|FINISH EXTRUSION(3,1)\|SALT MIGRATION(3,1)\|CENTRAL POSITION(2,4)\|SPIRAL SPRING(2,4)\|GROUND SECTION(2,3)\|ABSORBENT COTTON(2,1)\|ALKALI ION(2,1)\|ARTIFICIALLY PREPARED LEACHING SOLUTION(2,1)\|BICARBONATE(2,1)\|COLUMNAR SPONGE COMPRESSION RATIO(2,1)\|COLUMNAR SPONGE FLOW(2,1)\|DRENCHING SOLUTION(2,1)\|EVALUATION ERROR(2,1)\|EXCHANGE REACTION NA(2,1)\|EXTENSIVE TREATMENT(2,1)\|ION MIGRATION(2,1)\|KEY INDEX(2,1)\|MICROENVIRONMENT(2,1)\|OPENING END(2,1)\|PIPE CAVITY(2,1)\|SALINE ALKALI LAND(2,1)\|STABLE PROMOTION(2,1)\|SURFACE WATER SAMPLE(2,1)\|	(CN121253236)\|1. A buried soil water collection system, comprising:\| A fixed bracket; \| The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; \| the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; \| The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; \| a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and \|The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.\|2. The buried soil water collecting system according to claim 1, wherein the porous water absorbing material is a columnar sponge, an axial direction of the columnar sponge is parallel to an axial direction of the porous ceramic tube, and an outer peripheral surface of the columnar sponge is in contact with an inner side wall of the porous ceramic tube.\|3. The buried soil water collection system according to claim 2, wherein the extrusion assembly comprises a first pressing member slidably disposed in the porous ceramic tube, a second pressing member slidably disposed in the porous ceramic tube, an elastic member for elastically pressing the second pressing member against the first pressing member, and a push-pull rod for driving the first pressing member to slide against the second pressing member, the first pressing member is disposed adjacent to the closed end of the porous ceramic tube, the first pressing member is abutted against the first end of the columnar sponge, the second pressing member is disposed adjacent to the open end of the porous ceramic tube, the first pressing member is abutted against the second end of the columnar sponge, a first sliding hole for the push-pull rod to pass through is disposed on the second pressing member, a second sliding hole for the rod to pass through is disposed on the columnar sponge, the first end of the push-pull rod extends into the porous ceramic tube via the open end of the push-pull ceramic tube, and the first end of the push-pull rod is sequentially connected to the first sliding member after passing through the first sliding hole and the second sliding member.\|4. The buried soil water collecting system according to claim 3, wherein the elastic member is a coil spring accommodated in the porous ceramic tube, an opening end of the porous ceramic tube is provided with a holding cover for holding the coil spring, one end of the coil spring is held against and fixed on the holding cover, the other end of the coil spring is held against the second holding member, and a third sliding hole for the push-pull rod to pass through is formed in the holding cover.\|5. The system of claim 3, wherein the first pressing member comprises a first piston slidably disposed in the porous ceramic tube and a first pressing member connected to the first piston, wherein an outer circumferential surface of the first piston is in interference contact with an inner side wall of the porous ceramic tube, the first pressing member is in interference contact with a first end of the columnar sponge, and wherein the second pressing member comprises a second pressing member slidably disposed in the porous ceramic tube and connected to the second piston, wherein an outer circumferential surface of the second piston is in interference contact with an inner side wall of the porous ceramic tube, and wherein the second pressing member is in interference contact with a second end of the columnar sponge.\|6. The buried soil water collecting system according to claim 5, wherein the porous ceramic tube comprises a first tube section and a second tube section which are integrally formed, wherein one end of the first tube section away from the second tube section is a closed end, one end of the second tube section away from the first tube section is an open end, a microporous structure capable of adsorbing and transmitting soil water is arranged on a tube wall of the first tube section, the first piston and the columnar sponge are positioned in the first tube section, the tube wall of the second tube section is of a gas-tight and water-tight compact structure, the second piston and the elastic element are positioned in the second tube section, and the water outlet is arranged on the tube wall of the second tube section.\|7. A buried soil water collecting system according to claim 3, wherein a plurality of said soil water adsorbing members are provided in a plurality, said plurality of said soil water adsorbing members being arranged side by side and at intervals, each of said soil water adsorbing members being provided with one said pressing member, each of said pressing members being connected to said driving means.\|8. The buried soil water collecting system according to claim 7, wherein the driving device comprises a sliding rod, a driving rod and a cylinder, wherein the two ends of the sliding rod are respectively arranged on the fixed support in a sliding manner, the driving rod is used for driving the sliding rod to move along the axial direction of the sliding rod, the cylinder is used for driving the driving rod to move along the axial direction of the sliding rod, the axial direction of the sliding rod is perpendicular to the axial direction of the sliding rod, the second end of the sliding rod is connected with the sliding rod, the axial direction of the driving rod is parallel to the axial direction of the sliding rod, the first end of the driving rod is connected with the central position of the sliding rod, and the second end of the driving rod is connected with a piston rod of the cylinder.\|9. The buried soil water collecting system according to claim 8, wherein the number of the cylinders is two, piston rods of the two cylinders are symmetrically distributed by taking a central axis of the driving rod as a symmetrical axis, the driving device further comprises a connecting rod axially perpendicular to the axial direction of the driving rod and two pulley blocks symmetrically arranged on two sides of the driving rod, a pull rope is wound on each pulley block, the axial direction of a vertical section of each pull rope is parallel to the axial direction of the driving rod, one pull rope connects a first end of the sliding rod with a first end of the connecting rod, the other pull rope connects a second end of the sliding rod with a second end of the connecting rod, two ends of the connecting rod are respectively connected with the corresponding piston rods, and the second end of the driving rod is connected with a central position of the connecting rod.\|10. A buried soil water collecting system according to any one of claims 1 to 9 wherein said filter layer comprises at least one layer of non-woven fabric or silt filter screen.	(CN121253236)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reclamation and treatment, and particularly relates to a buried soil water collection system.\|BACKGROUND ART\|[0002] China is a large country of saline-alkali soil, and the third country is the first 10 countries in the area of saline-alkali soil. The Chinese saline-alkali soil is distributed in 17 provinces including northwest, northeast, north China and coastal areas, the total area of the saline-alkali barren lands and the saline-alkali lands affecting the cultivated lands exceeds 5 hundred million mu, and the agricultural production and the ecological safety are seriously restricted. In order to respond to the requirements of comprehensive treatment and comprehensive utilization of saline-alkali soil with stable promotion, development of a multifunctional silicate mineral conditioner with functions of improving saline-alkali soil, supplementing trace elements and fixing carbon is needed. The conditioner relies on the technology of enhancing silicate mineral weathering, and releases Ca 2+、Mg2+ and other exchange reactions Na +、CO2- 3、HCO-3 through mineral weathering, so that the salt and alkali ions are reduced, and simultaneously, the microelements of potassium, phosphorus, magnesium, zinc, selenium and other nutrients are released, and the fixation of atmospheric CO2 is realized in the mineral weathering-carbonate precipitation process.\|[0003] In the technical development process, a field-scale silicate mineral leaching weathering experiment is a key link for verifying mineral improvement effect and carbon sequestration potential. The weathering, ion migration and salt replacement processes of minerals in the soil take soil water as a main reaction medium, and the changes of cations, anions, dissolved inorganic carbon and other components in the soil water can directly reflect the weathering rate, the carbon fixation reaction process and the salt migration condition of the minerals. However, the prior art generally relies on manually formulating water or groundwater as a drenching solution, or employing surface runoff sampling instead of in situ soil water collection, which results in:\| 1) The weathering reaction condition is distorted, namely the artificially prepared leaching solution cannot accurately reproduce the pH value, the ionic strength and the organic acid content of the soil in the microenvironment, and the reality of mineral dissolution and carbonate precipitation reaction is affected; \| 2) The salt migration data is inaccurate, namely, the surface water sample is often influenced by evaporation, precipitation and surface pollution, and the real migration state of the salt with different depths of the section is difficult to reflect; \| 3) The carbon fixation amount has distortion and deviation, namely, the key indexes such as Dissolved Inorganic Carbon (DIC) and bicarbonate (HCO 3 -) in the in-situ soil water are lacked, so that the evaluation error of the carbon fixation amount is large. \|[0004] Therefore, in the research and product development of enhancing silicate mineral weathering for improvement of salty soil and carbon fixation, there is a need for a technical scheme capable of efficiently collecting real soil water samples under the condition of not damaging the in-situ structure and the moisture dynamics of soil so as to obtain reliable weathering reaction, salt replacement and carbon fixation process data and promote the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|[0005] The invention provides a buried soil water collecting system, which can collect soil water samples of different soil layers for a long time, stably and in situ under field conditions, and ensure that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for the mechanism research, the effect evaluation and the product optimization of the multifunctional silicate mineral conditioner in the application of improving and fixing the carbon of the saline soil.\|DISCLOSURE\|Disclosure of Invention\|[0006] Based on the above problems existing in the prior art, an object of the embodiments of the present invention is to provide a buried soil water collection system capable of efficiently collecting real soil water samples under the condition that the in-situ structure and the moisture dynamics of the soil are not damaged, so as to solve the technical problems in the prior art that soil water samples of different soil layers cannot be collected stably and in situ for a long time under the field condition, and chemical composition and hydraulic characteristics of the collected liquid are difficult to be ensured to be consistent with the soil environment.\|[0007] In order to achieve the above purpose, the invention adopts the technical scheme that the buried soil water collecting system comprises:\| A fixed bracket; \| The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; \| the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; \| The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; \| a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and \|The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.\|[0008] Further, the porous water absorbing material is a columnar sponge, the axial direction of the columnar sponge is parallel to the axial direction of the porous ceramic tube, and the outer peripheral surface of the columnar sponge is in contact with the inner side wall of the porous ceramic tube.\|[0009] Further, the extrusion assembly comprises a first abutting part arranged in the porous ceramic tube in a sliding manner, a second abutting part arranged in the porous ceramic tube in a sliding manner, an elastic part for elastically abutting the second abutting part towards the first abutting part, and a push-pull rod for driving the first abutting part to slide towards the second abutting part, wherein the first abutting part is arranged close to the closed end of the porous ceramic tube, the first abutting part is abutted against the first end of the columnar sponge, the second abutting part is arranged close to the opening end of the porous ceramic tube, the first abutting part is abutted against the second end of the columnar sponge, a first sliding hole for the push-pull rod to pass through is formed in the second abutting part, a second sliding hole for the push-pull rod to pass through is formed in the columnar sponge, the first end of the rod stretches into the porous ceramic tube through the opening end of the porous ceramic tube, and is connected with the first abutting part after sequentially passing through the first sliding hole and the second hole, and the first abutting part is connected with the second driving device.\|[0010] Further, the elastic piece is a spiral spring accommodated in the porous ceramic tube, an abutting cover for abutting against the spiral spring is arranged at the opening end of the porous ceramic tube, one end of the spiral spring abuts against and is fixed on the abutting cover, the other end of the spiral spring abuts against the second abutting piece, and a third sliding hole for the push-pull rod to pass through is formed in the abutting cover.\|[0011] Further, the first pressing piece comprises a first piston arranged in the porous ceramic tube in a sliding mode and a first pressing piece connected with the first piston, the outer peripheral surface of the first piston is in interference contact with the inner side wall of the porous ceramic tube, the first pressing piece is in interference contact with the first end of the columnar sponge, the second pressing piece comprises a second pressing piece connected with the second piston in the porous ceramic tube in a sliding mode, the outer peripheral surface of the second piston is in interference contact with the inner side wall of the porous ceramic tube, and the second pressing piece is in interference contact with the second end of the columnar sponge.\|[0012] Further, the porous ceramic pipe comprises a first pipe section and a second pipe section which are integrally formed, one end, away from the second pipe section, of the first pipe section is a closed end, one end, away from the first pipe section, of the second pipe section is an open end, a microporous structure capable of adsorbing and transmitting soil water is arranged on the pipe wall of the first pipe section, the first piston and the columnar sponge are located in the first pipe section, the pipe wall of the second pipe section is of an airtight and waterproof compact structure, the second piston and the elastic piece are located in the second pipe section, and the water outlet is formed in the pipe wall of the second pipe section.\|[0013] Further, the quantity of soil water adsorption components sets up to a plurality of, and is a plurality of soil water adsorption components just interval arrangement side by side, every soil water adsorption components is supporting to be set up one extrusion subassembly, every extrusion subassembly with drive arrangement links to each other.\|[0014] Further, the driving device comprises a sliding rod, a driving rod and a cylinder, wherein the two ends of the sliding rod are respectively arranged on the fixed support in a sliding mode, the driving rod is used for driving the sliding rod to move along the axial direction of the sliding rod, the cylinder is used for driving the driving rod to move along the axial direction, the axial direction of the sliding rod is perpendicular to the axial direction of the sliding rod, the second end of the sliding rod is connected with the sliding rod, the axial direction of the driving rod is parallel to the axial direction of the sliding rod, the first end of the driving rod is connected with the centering position of the sliding rod, and the second end of the driving rod is connected with a piston rod of the cylinder.\|[0015] Further, the number of the cylinders is two, piston rods of the two cylinders are symmetrically distributed by taking a central axis of the driving rod as a symmetrical axis, the driving device further comprises a connecting rod axially perpendicular to the axial direction of the driving rod and two pulley blocks symmetrically arranged on two sides of the driving rod, pull ropes are wound on each pulley block, the axial direction of a vertical section of each pull rope is parallel to the axial direction of the driving rod, one pull rope connects a first end of the sliding rod with a first end of the connecting rod, the other pull rope connects a second end of the sliding rod with a second end of the connecting rod, two ends of the connecting rod are respectively connected with corresponding piston rods, and the second end of the driving rod is connected with a centering position of the connecting rod.\|[0016] Further, the filter layer comprises at least one layer of non-woven fabrics or silt filter screens.\|[0017] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:\| According to the buried soil water collecting system provided by the embodiment of the invention, the porous ceramic pipe with the pipe wall having the micropore structure is buried in soil, the porous ceramic pipe is internally provided with the porous water absorbing material capable of absorbing and storing soil water and the extrusion component capable of extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic pipe under the capillary action, and is absorbed and transmitted to the porous water absorbing material through the micropore structure of the porous ceramic pipe, so that the porous water absorbing material can continuously absorb and store the soil water. And when the water storage amount in the porous water absorbing material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorbing material, so that the soil water stored in the porous water absorbing material is extruded, and the extruded soil water is drained to the water storage container through the water outlet holes and the liquid guide tube on the porous ceramic tube, so that the soil water is stored in the water storage container in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation. \|DRAWINGS DESCRIPTION\|[0018] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0019] FIG. 1 is a schematic perspective view of a buried soil water collection system according to the present invention;\| FIG. 2 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; \| FIG. 3 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; \| FIG. 4 is a schematic view of a buried soil water collection system according to the present invention buried in soil; \| FIG. 5 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in an uncompressed state according to the present invention; \| FIG. 6 is a cross-sectional view of the soil water adsorbing assembly and squeeze assembly of the present invention in an uncompressed state; \| FIG. 7 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in a squeezed state according to the present invention; \| FIG. 8 is a cross-sectional view of the soil water adsorbing assembly and the squeezing assembly according to the present invention in a squeezed state; \| fig. 9 is an exploded view of a soil water adsorbing assembly and a squeezing assembly according to the present invention. \|[0020] Wherein, each reference sign in the figure:\| 1-a fixed bracket, 11-a sliding groove; \| 2-a soil water adsorption component, 21-a porous ceramic tube, 211-a first tube section, 212-a second tube section, 213-a water outlet hole, 22-a porous water absorbing material, 221-a second sliding hole, 23-a supporting cover and 231-a third sliding hole; \| 3-extrusion assembly, 31-first pressing piece, 311-first piston, 312-first pressing piece, 32-second pressing piece, 321-second piston, 322-second pressing piece, 323-first sliding hole, 33-elastic piece and 34-push-pull rod; \| 4-driving device, 41-sliding rod, 42-driving rod, 43-cylinder, 431-piston rod, 44-pulley block, 441-fixed pulley, 442-movable pulley, 45-pull rope, 451-vertical section, 46-first pulley bracket, 47-second pulley bracket, 48-sliding chute or bar-shaped sliding hole and 49-connecting rod; \| a 5-liquid collecting system, a 51-water storage container, a 52-liquid guiding tube; \| 6-soil profile and 7-sliding shaft. \|INVENTION MODE\|Detailed Description\|[0021] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0022] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," "third," and "fourth" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first", "a second", "a third", and "a fourth" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0023] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.\|[0024] Referring to fig. 1 to 9, a description will be given of a buried soil water collecting system according to an embodiment of the present invention. Referring to fig. 1, 2 and 3 in combination, the buried soil water collecting system according to the embodiment of the present invention includes a fixing bracket 1, a soil water adsorbing assembly 2, an extruding assembly 3, a driving device 4, a liquid collecting system 5 and a filtering layer, wherein the fixing bracket 1 is used for fixing on one side of a soil profile 6, and is mainly used for supporting and fixing the whole buried soil water collecting system. The soil water adsorption assembly 2 is capable of adsorbing and storing soil water in soil by capillary action, the soil water adsorption assembly 2 comprises a porous ceramic tube 21 for burying the soil and a porous water absorbing material 22 arranged in the porous ceramic tube 21, a first end of the porous ceramic tube 21 is a closed end, the closed end of the porous ceramic tube 21 is in a conical structure so as to facilitate the insertion of the porous ceramic tube 21 into the soil, and a second end of the porous ceramic tube 21 is an open end. The position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is detachably connected or fixedly connected with the fixed support 1, and the position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is provided with a water outlet hole 213, and the water outlet hole 213 is communicated with the inner cavity of the porous ceramic tube 21. The porous ceramic tube 21 has a microporous structure on the wall, which can adsorb and transfer soil water in soil to the porous water absorbing material 22 by capillary action, the porous water absorbing material 22 has a continuous and mutually penetrating porous structure inside, and the porous water absorbing material 22 can adsorb and store a certain volume of soil water. The porous ceramic tube 21 has a cylindrical structure, and can ensure a maximum area of contact with the soil. Meanwhile, the porous water absorbing material 22 has a cylindrical structure, and can ensure contact with the inner tube wall of the porous ceramic tube 21 at a maximum area.\|[0025] The extrusion component 3 is movably arranged in the porous ceramic tube 21, and the extrusion component 3 is used for extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22, so that soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water flows out of the porous ceramic tube 21 through the water outlet holes 213 on the porous ceramic tube 21. The driving device 4 is arranged on the fixed bracket 1, the driving device 4 is connected with the extrusion assembly 3, and the driving device 4 is used for driving the extrusion assembly 3 to extrude the porous water absorbing material 22 according to a preset program or periodically, so that soil water stored in a continuous porous structure of the porous water absorbing material 22 is extruded. The liquid collecting system 5 includes a water storage container 51 for collecting soil water and a liquid guide tube 52 connecting the water storage container 51 with the water outlet 213, and the soil water flowing out through the water outlet 213 can be concentrated and stored in the water storage container 51 by drainage of the liquid guide tube 52. The filter layer wraps the outer side of the porous ceramic tube 21, and can allow soil water to permeate into the microporous structure of the porous ceramic tube 21, and meanwhile, the filter layer can block sediment in soil on the outer side of the porous ceramic tube 21, so that sediment in soil is blocked to block the microporous structure of the porous ceramic tube 21.\|[0026] Referring to fig. 4, a vertical section is excavated on one side of the soil to be taken, a porous ceramic tube 21 of a soil water adsorption component 2 is transversely inserted or buried into the soil through a soil section 6, a fixing support 1 is fixed on one side of the soil section 6, so that the porous ceramic tube 21 of the soil water adsorption component 2 cannot relatively displace with the soil, and a waterproof and airtight sealing film is paved on the soil surface and the soil section 6, wherein the sealing film can be, but is not limited to, a plastic film. In this way, the water (soil water) absorbed in the soil can permeate the filter layer, under the capillary action, the water is absorbed by the micropore structure of the porous ceramic tube 21 and is transmitted to the porous water absorbing material 22, the porous water absorbing material 22 continuously absorbs the soil water and continuously stores the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22, when the water storage capacity in the porous water absorbing material 22 reaches a certain value, the water storage capacity in the porous water absorbing material 22 can transmit a signal to the controller through the humidity sensor and/or the water content sensor, the controller controls the driving device 4 to work according to a preset program after receiving the signal, the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, and the soil water is concentrated and stored in the water storage container 51. After the soil water in the porous water absorbing material 22 is fully extruded, the controller controls the driving device 4 to stop working, at this time, the extrusion assembly 3 finishes the extrusion action on the porous water absorbing material 22, the porous water absorbing material 22 can recover the original state, continuously absorb the soil water again, and continuously store the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22 until the water storage amount in the porous water absorbing material 22 reaches a certain value, the controller can transmit signals to the controller through the humidity sensor and/or the water content sensor, after receiving the signals, the controller controls the driving device 4 to work according to a preset program, and the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded.\|[0027] Compared with the prior art, the buried soil water collecting system provided by the embodiment of the invention has the advantages that the porous ceramic tube 21 with the wall having the micropore structure is buried in soil, the porous water absorbing material 22 capable of absorbing and storing soil water and the extrusion component 3 capable of extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22 are arranged in the porous ceramic tube 21, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic tube 21 under the capillary action, and is absorbed and transmitted to the porous water absorbing material 22 through the micropore structure of the porous ceramic tube 21, so that the porous water absorbing material 22 can continuously absorb and store the soil water. Until the water storage amount in the porous water absorbing material 22 is sufficient, the squeezing component 3 is driven by the driving device 4 to squeeze the porous water absorbing material 22, so that the soil water stored in the porous water absorbing material 22 is squeezed out, and the squeezed soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, so that the soil water is stored in the water storage container 51 in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation.\|[0028] Referring to fig. 6, 8 and 9 in combination, in some embodiments, the porous water absorbing material 22 is a cylindrical sponge, the axial direction of the cylindrical sponge is parallel to the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the cylindrical sponge is in contact with the inner side wall of the porous ceramic tube 21. In this embodiment, the porous water absorbing material 22 is preferably a sponge with good water absorbing and storing properties, and the sponge is arranged in the porous ceramic tube 21 in a columnar shape, so that the axial direction of the columnar sponge is consistent with the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the columnar sponge is contacted with the inner side wall of the porous ceramic tube 21, thereby ensuring that the columnar sponge is contacted with the inner tube wall of the porous ceramic tube 21 in the largest area, and improving the adsorption and collection effects of soil water. In addition, the sponge is arranged in the porous ceramic tube 21 in a columnar shape, and is compressed from the axial direction of the columnar sponge through the extrusion component 3, so that on one hand, the compression ratio of the columnar sponge can be increased to fully extrude soil water in the columnar sponge, and the adsorption and collection efficiency of the soil water can be further improved, and on the other hand, when the extrusion component 3 finishes extrusion action on the columnar sponge, the columnar sponge is favorable for quickly recovering the original state, and then the soil water can be better adsorbed and stored later. The porous absorbent material 22 may be, but is not limited to, a sponge, and the porous absorbent material 22 may also be a porous material having a certain compression ratio, such as absorbent cotton, nonwoven fabric, or the like.\|[0029] Referring to fig. 6, 8 and 9, in some embodiments, the pressing assembly 3 includes a first pressing member 31 slidably disposed in the porous ceramic tube 21, a second pressing member 32 slidably disposed in the porous ceramic tube 21, an elastic member 33 for elastically pressing the second pressing member 32 toward the first pressing member 31, and a push-pull rod 34 for driving the first pressing member 31 to slide toward the second pressing member 32, wherein the first pressing member 31 is disposed adjacent to the closed end of the porous ceramic tube 21, the first pressing member 31 abuts against a first end of the columnar sponge, the second pressing member 32 is disposed adjacent to the open end of the porous ceramic tube 21, the first pressing member 31 abuts against a second end of the columnar sponge, a first sliding hole 323 for the push-pull rod 34 to pass through is disposed on the second pressing member 32, a second sliding hole 221 for the push-pull rod 34 to pass through is disposed on the columnar sponge, the first end of the rod 34 extends into the porous ceramic tube 21 through the open end of the porous ceramic tube 21, and is connected to the first sliding hole 323 and the second sliding hole 221 after sequentially passing through the first sliding hole and the second sliding hole 221, and the second pressing member 31 abuts against a second end of the columnar sponge, and the second end of the rod 34 is connected to the driving device 4. In this embodiment, the driving device 4 pulls the push-pull rod 34 towards the open end of the porous ceramic tube 21, the push-pull rod 34 drives the first pressing member 31 to move towards the second pressing member 32, and as the distance between the first pressing member 31 and the second pressing member 32 gradually decreases, the columnar sponge between the first pressing member 31 and the second pressing member 32 is continuously compressed, and the soil water in the columnar sponge is also continuously extruded in the compression process. In the process of pressing the columnar sponge by the first pressing piece 31 and the second pressing piece 32, the second pressing piece 32 is elastically pressed against the first pressing piece 31 by the elastic piece 33, so that soil water in the columnar sponge is slowly released under the elastic buffering action of the elastic piece 33, the columnar sponge is prevented from being excessively compressed by the first pressing piece 31 and the second pressing piece 32 instantly, the pressure in the porous ceramic tube 21 is instantly increased, the soil water can leak through the micropore structure of the porous ceramic, and the pH value and the ion concentration in the soil water can be changed. Because be equipped with the second slide hole 221 that supplies push-and-pull rod 34 to pass on the column sponge, the column sponge passes through second slide hole 221 cover and locates on the push-and-pull rod 34, in the in-process of first pressure piece 31 and the extrusion of second pressure piece 32 column sponge, not only can effectively avoid the column sponge that axial length is longer to take place distortion, can be favorable to the column sponge later stage to resume original state fast moreover. It should be noted that, a sealing ring is disposed between the push-pull rod 34 and the first sliding hole 323 to enhance the sealing performance of the sliding contact between the push-pull rod 34 and the first sliding hole 323. In addition, locate the column sponge between first pressure piece 31 and the second pressure piece 32 to push up the elasticity of second pressure piece 32 towards first pressure piece 31 through elastic component 33, on the one hand be favorable to high efficiency with the soil water extrusion in the column sponge, on the other hand can push back the column sponge to the position that adsorbs the soil water through the action of pushing up of elastic component 33 fast through the second pressure piece 32.\|[0030] Referring to fig. 5, 8 and 9 in combination, in some embodiments, the elastic member 33 is a coil spring accommodated in the porous ceramic tube 21, the open end of the porous ceramic tube 21 is provided with a holding cover 23 for holding the coil spring, one end of the coil spring is held against and fixed on the holding cover 23, the other end of the coil spring is held against the second holding member 32, the holding cover 23 is provided with a third sliding hole 231 through which the push-pull rod 34 passes, and a sealing ring is disposed between the push-pull rod 34 and the third sliding hole 231 to enhance the sealing performance of sliding contact between the push-pull rod 34 and the third sliding hole 231. It should be noted that the holding cover 23 may be, but not limited to, connected to the open end of the porous ceramic tube 21 by a threaded connection, and the elastic member 33 may be, but not limited to, a coil spring.\|[0031] Referring to fig. 6, 8 and 9, in some embodiments, the first pressing member 31 includes a first piston 311 slidably disposed in the porous ceramic tube 21 and a first pressing member 312 connected to the first piston 311, the outer peripheral surface of the first piston 311 is in interference contact with the inner sidewall of the porous ceramic tube 21, the first pressing member 312 abuts against the first end of the cylindrical sponge, the first piston 311 is a rubber member or a silicone member having elasticity, the first pressing member 312 is a hard metal sheet or a plastic sheet, and a supporting and reinforcing effect is formed on the first piston 311 by the first pressing member 312, so as to prevent the first pressing member 31 from deforming during the process of pressing the cylindrical spring. Similarly, the second pressing member 32 includes a second pressing member 322 slidably disposed in the porous ceramic tube 21 and connected to the second piston 321, where the outer circumferential surface of the second piston 321 is in interference contact with the inner sidewall of the porous ceramic tube 21, the second pressing member 322 abuts against the second end of the cylindrical sponge, the second piston 321 is a rubber member or a silica gel member having elasticity, and the second pressing member 322 is a hard metal sheet or a plastic sheet, and forms a supporting and reinforcing effect on the second piston 321 by the second pressing member 322, so as to prevent the deformation of the first pressing member 31 in the process of pressing the cylindrical spring.\|[0032] Referring to fig. 7, 8 and 9 in combination, in some embodiments, the porous ceramic tube 21 includes a first tube section 211 and a second tube section 212 that are integrally formed, one end of the first tube section 211 away from the second tube section 212 is a closed end, one end of the second tube section 212 away from the first tube section 211 is an open end, a microporous structure capable of adsorbing and transmitting soil water is provided on a tube wall of the first tube section 211, the first piston 311 and the columnar sponge are located in the first tube section 211, and the soil water can be adsorbed and transmitted to the columnar sponge in the first tube section 211 by capillary action of the microporous structure. Meanwhile, the pipe wall of the second pipe section 212 is of a dense structure which is airtight and watertight, and the second piston 321 and the elastic piece 33 are located in the second pipe section 212, so that the elastic piece 33 in the second pipe section 212 cannot pollute soil water, and meanwhile, the soil water cannot flow into the second pipe section 212 to erode the elastic piece 33. It should be noted that, when the first pressing member 31 drives the columnar sponge into the second pipe section 212, the elastic member 33 is in a compressed state, and the elastic member 33 can elastically press the second pressing member 32 against the first pressing member 31, so that the second pressing member 32 cooperates with the first pressing member 31 to compress the columnar sponge into the sealed second pipe cavity, and the soil water extruded from the columnar sponge flows out through the water outlet 213 on the pipe wall of the second pipe section 212. In addition, when the second pressing member 32 compresses the columnar sponge in the sealed second lumen in cooperation with the first pressing member 31, the pressure in the second tube section 212 can be increased, so that the soil water in the second tube section 212 is pressed out, and the collection efficiency of the soil water can be accelerated.\|[0033] Referring to fig. 1, 2 and 3, in some embodiments, in order to collect soil water more quickly and efficiently, a plurality of soil water adsorbing assemblies 2 are arranged, and a plurality of soil water adsorbing assemblies 2 are arranged side by side and at intervals, and each soil water adsorbing assembly 2 is provided with a squeezing assembly 3 in a matching manner, and each squeezing assembly 3 is connected with a driving device 4.\|[0034] Referring to fig. 1, 2 and 3, in some embodiments, the driving device 4 includes a sliding rod 41 with two ends slidably disposed on the fixed support 1, a driving rod 42 for driving the sliding rod 41 to move along the axial direction of the push-pull rod 34, and an air cylinder 43 for driving the driving rod 42 to move along the axial direction, the fixed support 1 is provided with a sliding groove 11, and two ends of the sliding rod 41 are slidably inserted into the sliding groove 11. The axial direction of the sliding rod 41 is perpendicular to the axial direction of the sliding rod 34, the second end of the sliding rod 34 is connected with the sliding rod 41, the axial direction of the driving rod 42 is parallel to the axial direction of the sliding rod 34, the first end of the driving rod 42 is connected with the central position of the sliding rod 34, and the second end of the driving rod 42 is connected with a piston rod 431 of the air cylinder 43. In this embodiment, the push-pull rod 34 is driven to axially move by the telescopic movement of the piston rod 431 of the air cylinder 43, so that the driving rod 42 can be driven to axially move along the driving rod 42 by the push-pull rod 34, the sliding rod 41 further drives the push-pull rod 34 to axially move, and the push-pull rod 34 drives the first pressing member 31 to reciprocate along the axial direction of the porous ceramic tube 21, so that the columnar sponge can be pressed by the first pressing member 31 and the second pressing member 32. It should be noted that, the fixed bracket 1 is provided with a sliding slot, two ends of the sliding rod 41 are respectively disposed in the corresponding sliding slots, the fixed bracket 1 is further provided with a fourth sliding hole, and the driving shaft is slidably inserted into the fourth sliding hole.\|[0035] Referring to fig. 1,2 and 3 in combination, in some embodiments, in order to enhance the stability of the movement of the push-pull rod 34 driven by the driving device 4 and to maintain the high precision operation of the push-pull rod 34, the number of the air cylinders 43 is two, the piston rods 431 of the two air cylinders 43 are symmetrically distributed with the central axis of the driving rod 42 as a symmetrical axis, the driving device 4 further comprises a connecting rod 49 axially perpendicular to the axial direction of the push-pull rod 34 and two pulley blocks 44 symmetrically arranged at two sides of the driving rod 42, each pulley block 44 is wound with a pull rope 45, the axial direction of the vertical section 451 of each pull rope 45 is parallel to the axial direction of the push-pull rod 34, one pull rope 45 connects the first end of the sliding rod 41 with the first end of the connecting rod 49, the other pull rope 45 connects the second end of the sliding rod 41 with the second end of the connecting rod 49, and the two ends of the connecting rod 49 are respectively connected with the corresponding piston rods 431, and the second end of the driving rod 42 is connected with the central position of the connecting rod 49. It should be noted that, each pulley block 44 includes at least one fixed pulley 441 and at least one movable pulley 442, the fixed pulley 441 is rotatably disposed on the fixed bracket 1 through the first pulley bracket 46, the first pulley bracket 46 is fixedly connected with the fixed bracket 1, the movable pulley 442 is rotatably disposed on the fixed bracket 1 through the second pulley bracket 47, and the second pulley bracket 47 is fixedly connected with the fixed bracket 1. Specifically, the fixed support 1 is provided with a second pulley support 47, the second pulley support 47 is provided with a sliding groove or a bar-shaped sliding hole 48 capable of guiding the movable pulley 442 to slide along the axial direction of the driving rod 42, and two sections of sliding shafts 7 respectively inserted into the sliding groove or the bar-shaped sliding hole 48, and the movable pulley 442 is slidably arranged on the guiding support 48 through a sliding matching structure of the sliding shafts 7 and the sliding groove or the bar-shaped sliding hole 48.\|[0036] It will be appreciated that in some embodiments, the filter layer comprises at least one layer of non-woven fabric, because the non-woven fabric has the advantages of being flexible, light in weight, non-toxic, easy to decompose, low in cost, and the like, the porous ceramic tube 21 can be effectively wrapped by the non-woven fabric as the filter layer, so that the pollution to soil water is avoided, the pollution to soil is low, and meanwhile, the cost of the buried soil water collecting system can be effectively controlled. Of course, the filter layer may also include at least one layer of sediment filter screen, and the filter layer may also be in other structural forms capable of blocking sediment outside the filter layer. It should be noted that the filter layer includes at least one layer of non-woven fabric or silt filter screen, which means that the filter layer wrapped on the outer side of the porous ceramic tube 21 may be a layer structure or a multi-layer structure, and is determined according to the filtering effects of different filtering materials and structures.\|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.	(CN121253236)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of rock weathering carbon fixation and saline soil reclamation and treatment, and particularly relates to a buried soil water collection system.\|BACKGROUND ART\|[0002] China is a large country of saline-alkali soil, and the third country is the first 10 countries in the area of saline-alkali soil. The Chinese saline-alkali soil is distributed in 17 provinces including northwest, northeast, north China and coastal areas, the total area of the saline-alkali barren lands and the saline-alkali lands affecting the cultivated lands exceeds 5 hundred million mu, and the agricultural production and the ecological safety are seriously restricted. In order to respond to the requirements of comprehensive treatment and comprehensive utilization of saline-alkali soil with stable promotion, development of a multifunctional silicate mineral conditioner with functions of improving saline-alkali soil, supplementing trace elements and fixing carbon is needed. The conditioner relies on the technology of enhancing silicate mineral weathering, and releases Ca 2+、Mg2+ and other exchange reactions Na +、CO2- 3、HCO-3 through mineral weathering, so that the salt and alkali ions are reduced, and simultaneously, the microelements of potassium, phosphorus, magnesium, zinc, selenium and other nutrients are released, and the fixation of atmospheric CO2 is realized in the mineral weathering-carbonate precipitation process.\|[0003] In the technical development process, a field-scale silicate mineral leaching weathering experiment is a key link for verifying mineral improvement effect and carbon sequestration potential. The weathering, ion migration and salt replacement processes of minerals in the soil take soil water as a main reaction medium, and the changes of cations, anions, dissolved inorganic carbon and other components in the soil water can directly reflect the weathering rate, the carbon fixation reaction process and the salt migration condition of the minerals. However, the prior art generally relies on manually formulating water or groundwater as a drenching solution, or employing surface runoff sampling instead of in situ soil water collection, which results in:\| 1) The weathering reaction condition is distorted, namely the artificially prepared leaching solution cannot accurately reproduce the pH value, the ionic strength and the organic acid content of the soil in the microenvironment, and the reality of mineral dissolution and carbonate precipitation reaction is affected; \| 2) The salt migration data is inaccurate, namely, the surface water sample is often influenced by evaporation, precipitation and surface pollution, and the real migration state of the salt with different depths of the section is difficult to reflect; \| 3) The carbon fixation amount has distortion and deviation, namely, the key indexes such as Dissolved Inorganic Carbon (DIC) and bicarbonate (HCO 3 -) in the in-situ soil water are lacked, so that the evaluation error of the carbon fixation amount is large. \|[0004] Therefore, in the research and product development of enhancing silicate mineral weathering for improvement of salty soil and carbon fixation, there is a need for a technical scheme capable of efficiently collecting real soil water samples under the condition of not damaging the in-situ structure and the moisture dynamics of soil so as to obtain reliable weathering reaction, salt replacement and carbon fixation process data and promote the authenticity of experimental simulation and the scientificity of research and development of mineral conditioning agents.\|[0005] The invention provides a buried soil water collecting system, which can collect soil water samples of different soil layers for a long time, stably and in situ under field conditions, and ensure that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for the mechanism research, the effect evaluation and the product optimization of the multifunctional silicate mineral conditioner in the application of improving and fixing the carbon of the saline soil.\|DISCLOSURE\|Disclosure of Invention\|[0006] Based on the above problems existing in the prior art, an object of the embodiments of the present invention is to provide a buried soil water collection system capable of efficiently collecting real soil water samples under the condition that the in-situ structure and the moisture dynamics of the soil are not damaged, so as to solve the technical problems in the prior art that soil water samples of different soil layers cannot be collected stably and in situ for a long time under the field condition, and chemical composition and hydraulic characteristics of the collected liquid are difficult to be ensured to be consistent with the soil environment.\|[0007] In order to achieve the above purpose, the invention adopts the technical scheme that the buried soil water collecting system comprises:\| A fixed bracket; \| The soil water adsorption component can adsorb and store soil water in soil through capillary action, the soil water adsorption component comprises a porous ceramic tube used for burying soil and a porous water absorption material arranged in the porous ceramic tube, the first end of the porous ceramic tube is a closed end, the second end of the porous ceramic tube is an open end, the position, close to the open end, of the porous ceramic tube is connected with the fixed support, the position, close to the open end, of the porous ceramic tube is provided with water outlet holes, the tube wall of the porous ceramic tube is provided with a micropore structure, the micropore structure can adsorb and transmit the soil water in the soil to the porous water absorption material through capillary action, and the porous water absorption material can adsorb and store the soil water; \| the extrusion component is used for extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material so that soil water stored in the continuous porous structure of the porous water absorbing material is extruded, and the extrusion component is movably arranged in the porous ceramic tube; \| The driving device is used for driving the extrusion assembly to extrude the porous water absorbing material, and is arranged on the fixed bracket; \| a liquid collecting system comprising a water storage container for collecting soil water and a liquid guide tube for connecting the water storage container with the water outlet hole, and \|The filter layer is wrapped on the outer side of the porous ceramic tube, and can allow the soil water to permeate into the microporous structure of the porous ceramic tube and block sediment in soil from blocking the microporous structure of the porous ceramic tube.\|[0008] Further, the porous water absorbing material is a columnar sponge, the axial direction of the columnar sponge is parallel to the axial direction of the porous ceramic tube, and the outer peripheral surface of the columnar sponge is in contact with the inner side wall of the porous ceramic tube.\|[0009] Further, the extrusion assembly comprises a first abutting part arranged in the porous ceramic tube in a sliding manner, a second abutting part arranged in the porous ceramic tube in a sliding manner, an elastic part for elastically abutting the second abutting part towards the first abutting part, and a push-pull rod for driving the first abutting part to slide towards the second abutting part, wherein the first abutting part is arranged close to the closed end of the porous ceramic tube, the first abutting part is abutted against the first end of the columnar sponge, the second abutting part is arranged close to the opening end of the porous ceramic tube, the first abutting part is abutted against the second end of the columnar sponge, a first sliding hole for the push-pull rod to pass through is formed in the second abutting part, a second sliding hole for the push-pull rod to pass through is formed in the columnar sponge, the first end of the rod stretches into the porous ceramic tube through the opening end of the porous ceramic tube, and is connected with the first abutting part after sequentially passing through the first sliding hole and the second hole, and the first abutting part is connected with the second driving device.\|[0010] Further, the elastic piece is a spiral spring accommodated in the porous ceramic tube, an abutting cover for abutting against the spiral spring is arranged at the opening end of the porous ceramic tube, one end of the spiral spring abuts against and is fixed on the abutting cover, the other end of the spiral spring abuts against the second abutting piece, and a third sliding hole for the push-pull rod to pass through is formed in the abutting cover.\|[0011] Further, the first pressing piece comprises a first piston arranged in the porous ceramic tube in a sliding mode and a first pressing piece connected with the first piston, the outer peripheral surface of the first piston is in interference contact with the inner side wall of the porous ceramic tube, the first pressing piece is in interference contact with the first end of the columnar sponge, the second pressing piece comprises a second pressing piece connected with the second piston in the porous ceramic tube in a sliding mode, the outer peripheral surface of the second piston is in interference contact with the inner side wall of the porous ceramic tube, and the second pressing piece is in interference contact with the second end of the columnar sponge.\|[0012] Further, the porous ceramic pipe comprises a first pipe section and a second pipe section which are integrally formed, one end, away from the second pipe section, of the first pipe section is a closed end, one end, away from the first pipe section, of the second pipe section is an open end, a microporous structure capable of adsorbing and transmitting soil water is arranged on the pipe wall of the first pipe section, the first piston and the columnar sponge are located in the first pipe section, the pipe wall of the second pipe section is of an airtight and waterproof compact structure, the second piston and the elastic piece are located in the second pipe section, and the water outlet is formed in the pipe wall of the second pipe section.\|[0013] Further, the quantity of soil water adsorption components sets up to a plurality of, and is a plurality of soil water adsorption components just interval arrangement side by side, every soil water adsorption components is supporting to be set up one extrusion subassembly, every extrusion subassembly with drive arrangement links to each other.\|[0014] Further, the driving device comprises a sliding rod, a driving rod and a cylinder, wherein the two ends of the sliding rod are respectively arranged on the fixed support in a sliding mode, the driving rod is used for driving the sliding rod to move along the axial direction of the sliding rod, the cylinder is used for driving the driving rod to move along the axial direction, the axial direction of the sliding rod is perpendicular to the axial direction of the sliding rod, the second end of the sliding rod is connected with the sliding rod, the axial direction of the driving rod is parallel to the axial direction of the sliding rod, the first end of the driving rod is connected with the centering position of the sliding rod, and the second end of the driving rod is connected with a piston rod of the cylinder.\|[0015] Further, the number of the cylinders is two, piston rods of the two cylinders are symmetrically distributed by taking a central axis of the driving rod as a symmetrical axis, the driving device further comprises a connecting rod axially perpendicular to the axial direction of the driving rod and two pulley blocks symmetrically arranged on two sides of the driving rod, pull ropes are wound on each pulley block, the axial direction of a vertical section of each pull rope is parallel to the axial direction of the driving rod, one pull rope connects a first end of the sliding rod with a first end of the connecting rod, the other pull rope connects a second end of the sliding rod with a second end of the connecting rod, two ends of the connecting rod are respectively connected with corresponding piston rods, and the second end of the driving rod is connected with a centering position of the connecting rod.\|[0016] Further, the filter layer comprises at least one layer of non-woven fabrics or silt filter screens.\|[0017] Compared with the prior art, the one or more technical schemes in the embodiment of the invention have at least one of the following beneficial effects:\| According to the buried soil water collecting system provided by the embodiment of the invention, the porous ceramic pipe with the pipe wall having the micropore structure is buried in soil, the porous ceramic pipe is internally provided with the porous water absorbing material capable of absorbing and storing soil water and the extrusion component capable of extruding the porous water absorbing material to adjust the compression ratio of the porous water absorbing material, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic pipe under the capillary action, and is absorbed and transmitted to the porous water absorbing material through the micropore structure of the porous ceramic pipe, so that the porous water absorbing material can continuously absorb and store the soil water. And when the water storage amount in the porous water absorbing material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorbing material, so that the soil water stored in the porous water absorbing material is extruded, and the extruded soil water is drained to the water storage container through the water outlet holes and the liquid guide tube on the porous ceramic tube, so that the soil water is stored in the water storage container in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation. \|DRAWINGS DESCRIPTION\|[0018] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0019] FIG. 1 is a schematic perspective view of a buried soil water collection system according to the present invention;\| FIG. 2 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; \| FIG. 3 is a schematic view of another perspective structure of the buried soil water collection system according to the present invention; \| FIG. 4 is a schematic view of a buried soil water collection system according to the present invention buried in soil; \| FIG. 5 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in an uncompressed state according to the present invention; \| FIG. 6 is a cross-sectional view of the soil water adsorbing assembly and squeeze assembly of the present invention in an uncompressed state; \| FIG. 7 is an assembly view of the soil water adsorbing assembly and the squeezing assembly in a squeezed state according to the present invention; \| FIG. 8 is a cross-sectional view of the soil water adsorbing assembly and the squeezing assembly according to the present invention in a squeezed state; \| fig. 9 is an exploded view of a soil water adsorbing assembly and a squeezing assembly according to the present invention. \|[0020] Wherein, each reference sign in the figure:\| 1-a fixed bracket, 11-a sliding groove; \| 2-a soil water adsorption component, 21-a porous ceramic tube, 211-a first tube section, 212-a second tube section, 213-a water outlet hole, 22-a porous water absorbing material, 221-a second sliding hole, 23-a supporting cover and 231-a third sliding hole; \| 3-extrusion assembly, 31-first pressing piece, 311-first piston, 312-first pressing piece, 32-second pressing piece, 321-second piston, 322-second pressing piece, 323-first sliding hole, 33-elastic piece and 34-push-pull rod; \| 4-driving device, 41-sliding rod, 42-driving rod, 43-cylinder, 431-piston rod, 44-pulley block, 441-fixed pulley, 442-movable pulley, 45-pull rope, 451-vertical section, 46-first pulley bracket, 47-second pulley bracket, 48-sliding chute or bar-shaped sliding hole and 49-connecting rod; \| a 5-liquid collecting system, a 51-water storage container, a 52-liquid guiding tube; \| 6-soil profile and 7-sliding shaft. \|INVENTION MODE\|Detailed Description\|[0021] In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.\|[0022] It will be understood that when an element is referred to as being "connected to" or "disposed on" another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element. Furthermore, the terms "first," "second," "third," and "fourth" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first", "a second", "a third", and "a fourth" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intervening medium, or in communication between two elements or in an interaction relationship between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0023] Reference throughout this specification to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present application. Thus, the appearances of the phrases "in one embodiment," "in some embodiments," or "in some embodiments" in various places throughout this specification are not all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.\|[0024] Referring to fig. 1 to 9, a description will be given of a buried soil water collecting system according to an embodiment of the present invention. Referring to fig. 1, 2 and 3 in combination, the buried soil water collecting system according to the embodiment of the present invention includes a fixing bracket 1, a soil water adsorbing assembly 2, an extruding assembly 3, a driving device 4, a liquid collecting system 5 and a filtering layer, wherein the fixing bracket 1 is used for fixing on one side of a soil profile 6, and is mainly used for supporting and fixing the whole buried soil water collecting system. The soil water adsorption assembly 2 is capable of adsorbing and storing soil water in soil by capillary action, the soil water adsorption assembly 2 comprises a porous ceramic tube 21 for burying the soil and a porous water absorbing material 22 arranged in the porous ceramic tube 21, a first end of the porous ceramic tube 21 is a closed end, the closed end of the porous ceramic tube 21 is in a conical structure so as to facilitate the insertion of the porous ceramic tube 21 into the soil, and a second end of the porous ceramic tube 21 is an open end. The position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is detachably connected or fixedly connected with the fixed support 1, and the position of the porous ceramic tube 21 close to the opening end of the porous ceramic tube 21 is provided with a water outlet hole 213, and the water outlet hole 213 is communicated with the inner cavity of the porous ceramic tube 21. The porous ceramic tube 21 has a microporous structure on the wall, which can adsorb and transfer soil water in soil to the porous water absorbing material 22 by capillary action, the porous water absorbing material 22 has a continuous and mutually penetrating porous structure inside, and the porous water absorbing material 22 can adsorb and store a certain volume of soil water. The porous ceramic tube 21 has a cylindrical structure, and can ensure a maximum area of contact with the soil. Meanwhile, the porous water absorbing material 22 has a cylindrical structure, and can ensure contact with the inner tube wall of the porous ceramic tube 21 at a maximum area.\|[0025] The extrusion component 3 is movably arranged in the porous ceramic tube 21, and the extrusion component 3 is used for extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22, so that soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water flows out of the porous ceramic tube 21 through the water outlet holes 213 on the porous ceramic tube 21. The driving device 4 is arranged on the fixed bracket 1, the driving device 4 is connected with the extrusion assembly 3, and the driving device 4 is used for driving the extrusion assembly 3 to extrude the porous water absorbing material 22 according to a preset program or periodically, so that soil water stored in a continuous porous structure of the porous water absorbing material 22 is extruded. The liquid collecting system 5 includes a water storage container 51 for collecting soil water and a liquid guide tube 52 connecting the water storage container 51 with the water outlet 213, and the soil water flowing out through the water outlet 213 can be concentrated and stored in the water storage container 51 by drainage of the liquid guide tube 52. The filter layer wraps the outer side of the porous ceramic tube 21, and can allow soil water to permeate into the microporous structure of the porous ceramic tube 21, and meanwhile, the filter layer can block sediment in soil on the outer side of the porous ceramic tube 21, so that sediment in soil is blocked to block the microporous structure of the porous ceramic tube 21.\|[0026] Referring to fig. 4, a vertical section is excavated on one side of the soil to be taken, a porous ceramic tube 21 of a soil water adsorption component 2 is transversely inserted or buried into the soil through a soil section 6, a fixing support 1 is fixed on one side of the soil section 6, so that the porous ceramic tube 21 of the soil water adsorption component 2 cannot relatively displace with the soil, and a waterproof and airtight sealing film is paved on the soil surface and the soil section 6, wherein the sealing film can be, but is not limited to, a plastic film. In this way, the water (soil water) absorbed in the soil can permeate the filter layer, under the capillary action, the water is absorbed by the micropore structure of the porous ceramic tube 21 and is transmitted to the porous water absorbing material 22, the porous water absorbing material 22 continuously absorbs the soil water and continuously stores the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22, when the water storage capacity in the porous water absorbing material 22 reaches a certain value, the water storage capacity in the porous water absorbing material 22 can transmit a signal to the controller through the humidity sensor and/or the water content sensor, the controller controls the driving device 4 to work according to a preset program after receiving the signal, the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded, and the extruded soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, and the soil water is concentrated and stored in the water storage container 51. After the soil water in the porous water absorbing material 22 is fully extruded, the controller controls the driving device 4 to stop working, at this time, the extrusion assembly 3 finishes the extrusion action on the porous water absorbing material 22, the porous water absorbing material 22 can recover the original state, continuously absorb the soil water again, and continuously store the absorbed soil water in the continuous and mutually penetrated porous structure inside the porous water absorbing material 22 until the water storage amount in the porous water absorbing material 22 reaches a certain value, the controller can transmit signals to the controller through the humidity sensor and/or the water content sensor, after receiving the signals, the controller controls the driving device 4 to work according to a preset program, and the driving device 4 drives the extrusion assembly 3 to extrude the porous water absorbing material 22, so that the soil water stored in the continuous porous structure of the porous water absorbing material 22 is extruded.\|[0027] Compared with the prior art, the buried soil water collecting system provided by the embodiment of the invention has the advantages that the porous ceramic tube 21 with the wall having the micropore structure is buried in soil, the porous water absorbing material 22 capable of absorbing and storing soil water and the extrusion component 3 capable of extruding the porous water absorbing material 22 to adjust the compression ratio of the porous water absorbing material 22 are arranged in the porous ceramic tube 21, the soil water absorbed in the soil can pass through the filter layer wrapped on the outer side of the porous ceramic tube 21 under the capillary action, and is absorbed and transmitted to the porous water absorbing material 22 through the micropore structure of the porous ceramic tube 21, so that the porous water absorbing material 22 can continuously absorb and store the soil water. Until the water storage amount in the porous water absorbing material 22 is sufficient, the squeezing component 3 is driven by the driving device 4 to squeeze the porous water absorbing material 22, so that the soil water stored in the porous water absorbing material 22 is squeezed out, and the squeezed soil water is drained to the water storage container 51 through the water outlet 213 and the liquid guide tube 52 on the porous ceramic tube 21, so that the soil water is stored in the water storage container 51 in a concentrated manner. Therefore, the buried soil water collecting system provided by the embodiment of the invention can be used for efficiently collecting the real soil water sample under the condition that the in-situ structure and the moisture dynamic state of the soil are not damaged. In addition, the buried soil water collecting system provided by the embodiment of the invention can reduce the difficulty of collecting in-situ soil water, can not collect soil water samples of different soil layers in situ stably and efficiently for a long time under field conditions, and ensures that the chemical composition and the hydraulic characteristics of the collected liquid are consistent with those of the soil environment, thereby providing accurate and repeatable experimental data support for mechanism research, effect evaluation and product optimization of the multifunctional silicate mineral conditioner in the application of salinized soil improvement and carbon fixation.\|[0028] Referring to fig. 6, 8 and 9 in combination, in some embodiments, the porous water absorbing material 22 is a cylindrical sponge, the axial direction of the cylindrical sponge is parallel to the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the cylindrical sponge is in contact with the inner side wall of the porous ceramic tube 21. In this embodiment, the porous water absorbing material 22 is preferably a sponge with good water absorbing and storing properties, and the sponge is arranged in the porous ceramic tube 21 in a columnar shape, so that the axial direction of the columnar sponge is consistent with the axial direction of the porous ceramic tube 21, and the outer peripheral surface of the columnar sponge is contacted with the inner side wall of the porous ceramic tube 21, thereby ensuring that the columnar sponge is contacted with the inner tube wall of the porous ceramic tube 21 in the largest area, and improving the adsorption and collection effects of soil water. In addition, the sponge is arranged in the porous ceramic tube 21 in a columnar shape, and is compressed from the axial direction of the columnar sponge through the extrusion component 3, so that on one hand, the compression ratio of the columnar sponge can be increased to fully extrude soil water in the columnar sponge, and the adsorption and collection efficiency of the soil water can be further improved, and on the other hand, when the extrusion component 3 finishes extrusion action on the columnar sponge, the columnar sponge is favorable for quickly recovering the original state, and then the soil water can be better adsorbed and stored later. The porous absorbent material 22 may be, but is not limited to, a sponge, and the porous absorbent material 22 may also be a porous material having a certain compression ratio, such as absorbent cotton, nonwoven fabric, or the like.\|[0029] Referring to fig. 6, 8 and 9, in some embodiments, the pressing assembly 3 includes a first pressing member 31 slidably disposed in the porous ceramic tube 21, a second pressing member 32 slidably disposed in the porous ceramic tube 21, an elastic member 33 for elastically pressing the second pressing member 32 toward the first pressing member 31, and a push-pull rod 34 for driving the first pressing member 31 to slide toward the second pressing member 32, wherein the first pressing member 31 is disposed adjacent to the closed end of the porous ceramic tube 21, the first pressing member 31 abuts against a first end of the columnar sponge, the second pressing member 32 is disposed adjacent to the open end of the porous ceramic tube 21, the first pressing member 31 abuts against a second end of the columnar sponge, a first sliding hole 323 for the push-pull rod 34 to pass through is disposed on the second pressing member 32, a second sliding hole 221 for the push-pull rod 34 to pass through is disposed on the columnar sponge, the first end of the rod 34 extends into the porous ceramic tube 21 through the open end of the porous ceramic tube 21, and is connected to the first sliding hole 323 and the second sliding hole 221 after sequentially passing through the first sliding hole and the second sliding hole 221, and the second pressing member 31 abuts against a second end of the columnar sponge, and the second end of the rod 34 is connected to the driving device 4. In this embodiment, the driving device 4 pulls the push-pull rod 34 towards the open end of the porous ceramic tube 21, the push-pull rod 34 drives the first pressing member 31 to move towards the second pressing member 32, and as the distance between the first pressing member 31 and the second pressing member 32 gradually decreases, the columnar sponge between the first pressing member 31 and the second pressing member 32 is continuously compressed, and the soil water in the columnar sponge is also continuously extruded in the compression process. In the process of pressing the columnar sponge by the first pressing piece 31 and the second pressing piece 32, the second pressing piece 32 is elastically pressed against the first pressing piece 31 by the elastic piece 33, so that soil water in the columnar sponge is slowly released under the elastic buffering action of the elastic piece 33, the columnar sponge is prevented from being excessively compressed by the first pressing piece 31 and the second pressing piece 32 instantly, the pressure in the porous ceramic tube 21 is instantly increased, the soil water can leak through the micropore structure of the porous ceramic, and the pH value and the ion concentration in the soil water can be changed. Because be equipped with the second slide hole 221 that supplies push-and-pull rod 34 to pass on the column sponge, the column sponge passes through second slide hole 221 cover and locates on the push-and-pull rod 34, in the in-process of first pressure piece 31 and the extrusion of second pressure piece 32 column sponge, not only can effectively avoid the column sponge that axial length is longer to take place distortion, can be favorable to the column sponge later stage to resume original state fast moreover. It should be noted that, a sealing ring is disposed between the push-pull rod 34 and the first sliding hole 323 to enhance the sealing performance of the sliding contact between the push-pull rod 34 and the first sliding hole 323. In addition, locate the column sponge between first pressure piece 31 and the second pressure piece 32 to push up the elasticity of second pressure piece 32 towards first pressure piece 31 through elastic component 33, on the one hand be favorable to high efficiency with the soil water extrusion in the column sponge, on the other hand can push back the column sponge to the position that adsorbs the soil water through the action of pushing up of elastic component 33 fast through the second pressure piece 32.\|[0030] Referring to fig. 5, 8 and 9 in combination, in some embodiments, the elastic member 33 is a coil spring accommodated in the porous ceramic tube 21, the open end of the porous ceramic tube 21 is provided with a holding cover 23 for holding the coil spring, one end of the coil spring is held against and fixed on the holding cover 23, the other end of the coil spring is held against the second holding member 32, the holding cover 23 is provided with a third sliding hole 231 through which the push-pull rod 34 passes, and a sealing ring is disposed between the push-pull rod 34 and the third sliding hole 231 to enhance the sealing performance of sliding contact between the push-pull rod 34 and the third sliding hole 231. It should be noted that the holding cover 23 may be, but not limited to, connected to the open end of the porous ceramic tube 21 by a threaded connection, and the elastic member 33 may be, but not limited to, a coil spring.\|[0031] Referring to fig. 6, 8 and 9, in some embodiments, the first pressing member 31 includes a first piston 311 slidably disposed in the porous ceramic tube 21 and a first pressing member 312 connected to the first piston 311, the outer peripheral surface of the first piston 311 is in interference contact with the inner sidewall of the porous ceramic tube 21, the first pressing member 312 abuts against the first end of the cylindrical sponge, the first piston 311 is a rubber member or a silicone member having elasticity, the first pressing member 312 is a hard metal sheet or a plastic sheet, and a supporting and reinforcing effect is formed on the first piston 311 by the first pressing member 312, so as to prevent the first pressing member 31 from deforming during the process of pressing the cylindrical spring. Similarly, the second pressing member 32 includes a second pressing member 322 slidably disposed in the porous ceramic tube 21 and connected to the second piston 321, where the outer circumferential surface of the second piston 321 is in interference contact with the inner sidewall of the porous ceramic tube 21, the second pressing member 322 abuts against the second end of the cylindrical sponge, the second piston 321 is a rubber member or a silica gel member having elasticity, and the second pressing member 322 is a hard metal sheet or a plastic sheet, and forms a supporting and reinforcing effect on the second piston 321 by the second pressing member 322, so as to prevent the deformation of the first pressing member 31 in the process of pressing the cylindrical spring.\|[0032] Referring to fig. 7, 8 and 9 in combination, in some embodiments, the porous ceramic tube 21 includes a first tube section 211 and a second tube section 212 that are integrally formed, one end of the first tube section 211 away from the second tube section 212 is a closed end, one end of the second tube section 212 away from the first tube section 211 is an open end, a microporous structure capable of adsorbing and transmitting soil water is provided on a tube wall of the first tube section 211, the first piston 311 and the columnar sponge are located in the first tube section 211, and the soil water can be adsorbed and transmitted to the columnar sponge in the first tube section 211 by capillary action of the microporous structure. Meanwhile, the pipe wall of the second pipe section 212 is of a dense structure which is airtight and watertight, and the second piston 321 and the elastic piece 33 are located in the second pipe section 212, so that the elastic piece 33 in the second pipe section 212 cannot pollute soil water, and meanwhile, the soil water cannot flow into the second pipe section 212 to erode the elastic piece 33. It should be noted that, when the first pressing member 31 drives the columnar sponge into the second pipe section 212, the elastic member 33 is in a compressed state, and the elastic member 33 can elastically press the second pressing member 32 against the first pressing member 31, so that the second pressing member 32 cooperates with the first pressing member 31 to compress the columnar sponge into the sealed second pipe cavity, and the soil water extruded from the columnar sponge flows out through the water outlet 213 on the pipe wall of the second pipe section 212. In addition, when the second pressing member 32 compresses the columnar sponge in the sealed second lumen in cooperation with the first pressing member 31, the pressure in the second tube section 212 can be increased, so that the soil water in the second tube section 212 is pressed out, and the collection efficiency of the soil water can be accelerated.\|[0033] Referring to fig. 1, 2 and 3, in some embodiments, in order to collect soil water more quickly and efficiently, a plurality of soil water adsorbing assemblies 2 are arranged, and a plurality of soil water adsorbing assemblies 2 are arranged side by side and at intervals, and each soil water adsorbing assembly 2 is provided with a squeezing assembly 3 in a matching manner, and each squeezing assembly 3 is connected with a driving device 4.\|[0034] Referring to fig. 1, 2 and 3, in some embodiments, the driving device 4 includes a sliding rod 41 with two ends slidably disposed on the fixed support 1, a driving rod 42 for driving the sliding rod 41 to move along the axial direction of the push-pull rod 34, and an air cylinder 43 for driving the driving rod 42 to move along the axial direction, the fixed support 1 is provided with a sliding groove 11, and two ends of the sliding rod 41 are slidably inserted into the sliding groove 11. The axial direction of the sliding rod 41 is perpendicular to the axial direction of the sliding rod 34, the second end of the sliding rod 34 is connected with the sliding rod 41, the axial direction of the driving rod 42 is parallel to the axial direction of the sliding rod 34, the first end of the driving rod 42 is connected with the central position of the sliding rod 34, and the second end of the driving rod 42 is connected with a piston rod 431 of the air cylinder 43. In this embodiment, the push-pull rod 34 is driven to axially move by the telescopic movement of the piston rod 431 of the air cylinder 43, so that the driving rod 42 can be driven to axially move along the driving rod 42 by the push-pull rod 34, the sliding rod 41 further drives the push-pull rod 34 to axially move, and the push-pull rod 34 drives the first pressing member 31 to reciprocate along the axial direction of the porous ceramic tube 21, so that the columnar sponge can be pressed by the first pressing member 31 and the second pressing member 32. It should be noted that, the fixed bracket 1 is provided with a sliding slot, two ends of the sliding rod 41 are respectively disposed in the corresponding sliding slots, the fixed bracket 1 is further provided with a fourth sliding hole, and the driving shaft is slidably inserted into the fourth sliding hole.\|[0035] Referring to fig. 1,2 and 3 in combination, in some embodiments, in order to enhance the stability of the movement of the push-pull rod 34 driven by the driving device 4 and to maintain the high precision operation of the push-pull rod 34, the number of the air cylinders 43 is two, the piston rods 431 of the two air cylinders 43 are symmetrically distributed with the central axis of the driving rod 42 as a symmetrical axis, the driving device 4 further comprises a connecting rod 49 axially perpendicular to the axial direction of the push-pull rod 34 and two pulley blocks 44 symmetrically arranged at two sides of the driving rod 42, each pulley block 44 is wound with a pull rope 45, the axial direction of the vertical section 451 of each pull rope 45 is parallel to the axial direction of the push-pull rod 34, one pull rope 45 connects the first end of the sliding rod 41 with the first end of the connecting rod 49, the other pull rope 45 connects the second end of the sliding rod 41 with the second end of the connecting rod 49, and the two ends of the connecting rod 49 are respectively connected with the corresponding piston rods 431, and the second end of the driving rod 42 is connected with the central position of the connecting rod 49. It should be noted that, each pulley block 44 includes at least one fixed pulley 441 and at least one movable pulley 442, the fixed pulley 441 is rotatably disposed on the fixed bracket 1 through the first pulley bracket 46, the first pulley bracket 46 is fixedly connected with the fixed bracket 1, the movable pulley 442 is rotatably disposed on the fixed bracket 1 through the second pulley bracket 47, and the second pulley bracket 47 is fixedly connected with the fixed bracket 1. Specifically, the fixed support 1 is provided with a second pulley support 47, the second pulley support 47 is provided with a sliding groove or a bar-shaped sliding hole 48 capable of guiding the movable pulley 442 to slide along the axial direction of the driving rod 42, and two sections of sliding shafts 7 respectively inserted into the sliding groove or the bar-shaped sliding hole 48, and the movable pulley 442 is slidably arranged on the guiding support 48 through a sliding matching structure of the sliding shafts 7 and the sliding groove or the bar-shaped sliding hole 48.\|[0036] It will be appreciated that in some embodiments, the filter layer comprises at least one layer of non-woven fabric, because the non-woven fabric has the advantages of being flexible, light in weight, non-toxic, easy to decompose, low in cost, and the like, the porous ceramic tube 21 can be effectively wrapped by the non-woven fabric as the filter layer, so that the pollution to soil water is avoided, the pollution to soil is low, and meanwhile, the cost of the buried soil water collecting system can be effectively controlled. Of course, the filter layer may also include at least one layer of sediment filter screen, and the filter layer may also be in other structural forms capable of blocking sediment outside the filter layer. It should be noted that the filter layer includes at least one layer of non-woven fabric or silt filter screen, which means that the filter layer wrapped on the outer side of the porous ceramic tube 21 may be a layer structure or a multi-layer structure, and is determined according to the filtering effects of different filtering materials and structures.\|[0037] The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.	Family Number\|(117274553)\|117274553\|Object of Invention\|(CN121253236 A)\|The invention provides a buried soil water collecting system , which belongs to the technical field of rock weathering carbon fixation and saline soil reconstruction and treatment , wherein a porous ceramic tube is buried in soil , a porous water absorbing material and an extrusion component for extruding the porous water absorbing material are arranged in the ( . . . ) \|Abstract\|(CN121253236 A)\|The invention provides a buried soil water collection system , and belongs to the technical field of rock weathering carbon sequestration and salinized soil transformation and governance , a porous ceramic tube is buried in soil , a porous water absorption material and an extrusion assembly for extruding the porous water absorption material are arranged in the porous ceramic tube , and soil water adsorbed in the soil is absorbed by the porous ceramic tube under the capillary action , so that the soil water is absorbed by the porous ceramic tube ; the soil water is adsorbed and transmitted to the porous water absorption material through the microporous structure of the porous ceramic tube , and the porous water absorption material can continuously adsorb and store the soil water . When the water storage amount in the porous water absorption material is sufficient , the extrusion assembly is driven by the driving device to extrude the porous water absorption material , so that the soil water stored in the porous water absorption material is extruded out , and the extruded soil water is drained to the water storage container through the water outlet holes in the porous ceramic pipe and the liquid guide pipe , so that the soil water is centrally stored in the water storage container . Therefore , the real soil water sample can be stably and efficiently collected for a long time under the field condition that the in - situ structure and the moisture dynamic state of the soil are not damaged . \|	Measurement	G01N-001/20\|G01N-001/20/35\|G01N-2001/2021\|G01N-2001/205		G01N-001/20\|G01N-001/20/35\|G01N-2001/2021\|G01N-2001/205	G01N-001/20	G01N-001/20										PENDING	(CN121253236)\|PENDING	ALIVE	(CN121253236)\|ALIVE	(CN121253236)\|LEGAL DETAILS FOR CN121253236\|Actual or expected expiration date=2045-10-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-10-29\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202511559558\|Application date=2025-10-29\|Standardized application number=2025CN-1559558\|Event publication date=2026-01-02\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN121253236\|Publication stage code=A\|Publication date=2026-01-02\|Standardized publication number=CN121253236\|Event publication date=2026-01-02\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2026-01-20\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN121253236)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=r6DqxGvtRKfJWdolE5dLe1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000080386811&ekey=1806&xpn=CN121253236&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=gPZaP4yiAL%252BirZpns%252Bzw6pNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN121253236)\|CN	(CN121253236)\|NAME=LANZHOU UNIVERSITY , COUNTRY=CN		(CN121253236)\|NAME=HE PENG;SHENZHEN LIYU INTELLECTUAPROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=41028	(CN121253236)\|CN	(CN121253236)\|NAME=ZHANG JIETANG, COUNTRY=CN \|NAME=LI XINGYUAN\|NAME=GOU XIAOHUA	(CN121253236)\|9	1	1					(CN121253236)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2026-01-02\|Gazette number: GAZNUM=42-0101\|Number of Pages: NPAGES=21\|		(CN121253236)\|CHINESE (CHI)	(CN121253236)\|Patent	Titre: (CN121253236)\|Buried soil water collecting system Résumé: (CN121253236)\|The invention provides a buried soil water collection system, and belongs to the technical field of rock weathering carbon sequestration and salinized soil transformation and governance, a porous ceramic tube is buried in soil, a porous water absorption material and an extrusion assembly for extruding the porous water absorption material are arranged in the porous ceramic tube, and soil water adsorbed in the soil is absorbed by the porous ceramic tube under the capillary action, so that the soil water is absorbed by the porous ceramic tube; the soil water is adsorbed and transmitted to the porous water absorption material through the microporous structure of the porous ceramic tube, and the porous water absorption material can continuously adsorb and store the soil water. When the water storage amount in the porous water absorption material is sufficient, the extrusion assembly is driven by the driving device to extrude the porous water absorption material, so that the soil water stored in the porous water absorption material is extruded out, and the extruded soil water is drained to the water storage container through the water outlet holes in the porous ceramic pipe and the liquid guide pipe, so that the soil water is centrally stored in the water storage container. Therefore, the real soil water sample can be stably and efficiently collected for a long time under the field condition that the in-situ structure and the moisture dynamic state of the soil are not damaged.	19	Abstract	gpt-4o-mini	no	The article focuses on a soil water collection system and does not address accelerated weathering or CO₂ capture.
21	CN202210073314	CN202211317927\|CN202210073314	CN115445393\|CN115445393\|CN114522512	100174807	CN115445393 B 2024-04-26 [CN115445393B]\|CN115445393 A 2022-12-09 [CN115445393]\|CN114522512 A 2022-05-24 [CN114522512]	2022-01-21	2022-10-26\|2022-01-21	2024-04-26\|2022-12-09\|2022-05-24	(CN115445393B)\|2024-04-26\|	(CN115445393)\|2042-10-26\|(CN114522512)\|2022-12-06	(CN115445393)\|Method for improving carbon sink efficiency of soil and underground water	(CN115445393)\|The invention discloses a method for improving the carbon sink efficiency of soil and underground water, and relates to the technical field of carbon sink increase and carbon cycle improvement. The method comprises the following steps: step 1, judging and extracting a main rainfall infiltration supply area through site GIS analysis and DEM three-dimensional model, and taking the main rainfall infiltration supply area as an area for increasing the rainfall infiltration amount; step 2, paving peat soil with a high-adsorbability and high-water-content space to the area selected in the step 1, and wetting the dried peat soil with water before paving; thirdly, holes are formed in the laid peat soil, the permeability of a laid area is enhanced, more earth surface rainfall can enter the soil and underground water space through infiltration, and the CO2 amount adsorbed by the peat soil is increased. Through soil adsorption and rainfall infiltration leaching carrying processes, the content of dissolved inorganic carbon entering the soil and underground water is greatly increased, so that atmospheric CO2 is stored in a deep underground space, the carbon sequestration efficiency of the soil and underground water is improved, and important carbon sequestration significance is achieved.	GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN	(CN115445393)\|GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY ([CN])\|(CN115445393)\|GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY ([CN])\|(CN114522512)\|GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY ([CN])	YANG MINGXING\|ZHANG MIN\|YANG WU\|XIE FEI\|YAO DUNTING\|LI WEI	(CN115445393)\|YANG MINGXING\|ZHANG MIN\|YANG WU\|XIE FEI\|YAO DUNTING\|LI WEI\|(CN115445393)\|YANG MINGXING\|ZHANG MIN\|YANG WU\|XIE FEI\|YAO DUNTING\|LI WEI	(CN115445393)\|CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP)\|Reg. Nb: 11308\|(CN114522512)\|CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP)\|Reg. Nb: 11308	(CN115445393)\|Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.\|In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples.\|	(CN115445393)\|1. A method for improving the carbon sink efficiency of soil and underground water is characterized by comprising the following steps: the method comprises the following steps: Firstly, judging and extracting a main rainfall infiltration supplementing area through site GIS analysis and a DEM three-dimensional model to serve as an area for increasing rainfall infiltration; secondly, spreading peat soil with high adsorptivity and high water content to the area selected in the first step, and wetting the dried peat soil with water before spreading; thirdly, inserting holes in the peat soil which is well paved, enhancing the permeability of the paved area, and enabling more surface rainfall to enter soil and groundwater space through infiltration so as to increase the CO 2 absorbed by the peat soil; And fourthly, increasing the water infiltration amount by adopting a manual sprinkling or leaching mode in a rainfall-free season, increasing the CO 2 amount adsorbed by peat soil, and absorbing and storing atmospheric CO 2 in soil and underground water to form dissolved inorganic carbon so as to realize the purpose of carbon sink. \|	(CN115445393)\|The invention aims to provide a technology for improving carbon sink efficiency of soil and underground water, which is used for improving the carbon sink efficiency of the soil and the underground water for absorbing and storing CO 2 by improving the performance of the soil for absorbing CO 2 and according to the combination form of CO 2 and water in the surface process and the flow circulation mode, and solving the problems in the background technology.\|The invention discloses a method for improving carbon sink efficiency of soil and underground water, and relates to the technical field of carbon sink increasing and carbon circulation improving.\|The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps:\|	(CN115445393)\|GROUND(100,34)\|CARBON SINK(100,29)\|UNDERGROUND WATER(100,18)\|RAINFALL INFILTRATION(100,10)\|RAINFALL INFILTRATION REPLENISHMENT ZONE(66,1)\|RAINFALL INFILTRATION LEACHING(61,2)\|SPREADING PEAT SOIL(55,6)\|GROUNDWATER(45,12)\|SITE GI ANALYSIS(44,4)\|PEAT SOIL DRYING(43,6)\|PEAT SOIL(42,22)\|ADSORPTIVITY(40,6)\|SITE GI(37,4)\|INSERTION(36,4)\|SPRINKLING(36,1)\|SOIL PERFORMANCE(33,1)\|INFILTRATION(31,7)\|CARBON CIRCULATION(30,2)\|PAVED AREA(29,2)\|TILED PEAT SOIL(29,2)\|PEAT SOIL WETTING(28,2)\|SOIL CARBON SEQUESTRATION(25,1)\|LEACHING MODE(24,3)\|COLLECTION ZONE(22,1)\|RAINFALL FREE SEASON(21,3)\|SURFACE RAINFALL(19,6)\|DEM THREE DIMENSIONAL MODEL(18,4)\|HCO3 ION(18,4)\|CARBON SINK SIGNIFICANCE(18,2)\|PAVING THICKNESS(18,2)\|FLOW CIRCULATION MODE(17,1)\|GULLY(14,2)\|SOIL ADSORPTION(14,2)\|DEEP UNDERGROUND SPACE(13,4)\|DEPRESSION(12,4)\|WATER INFILTRATION(12,3)\|3D MODEL(11,4)\|DISSOLVED INORGANIC CARBON(10,15)\|PAVED REGION PERMEABILITY(10,2)\|SOIL RAINFALL INFILTRATION CHANNEL(10,1)\|RAINFALL INFILTRATION FLUSHING ACTION(9,1)\|RAINFALL SURFACE RUNOFF(8,7)\|SOIL PHYSICAL MODIFIER(8,2)\|DISSOLVED INORGANIC CARBON CONTENT(7,3)\|SOIL ADSORPTION CAPACITY(7,1)\|RAINFALL INFILTRATION SUPPLY AREA(6,4)\|WELL PAVED PEAT SOIL(6,2)\|ADSORPTIVE ABSORPTION(6,1)\|ATMOSPHERIC RAINFALL(6,1)\|CARBON SINK ECONOMIC PROSPECT(6,1)\|RAINFALL INFILTRATION REPLENISHMENT AREA(6,1)\|SOIL ADSORPTION PERFORMANCE(6,1)\|COLLECTION AREA(5,6)\|POROSITY(5,3)\|CARBON NEUTRALIZATION(5,2)\|FORMED INSERTION HOLE(5,2)\|SPRINKLING MODE(5,2)\|ECONOMY DEVELOPMENT(5,1)\|RAINFALL INFILTRATION CAPACITY(5,1)\|DITCH(4,2)\|SPREADING THICKNESS(4,2)\|STAINLESS STEEL STICK(4,2)\|\|(CN115445393)\|GROUND(100,44)\|UNDERGROUND WATER(100,26)\|CARBON SEQUESTRATION(100,13)\|PRECIPITATION INFILTRATION(100,1)\|LEAD PRECIPITATION INFILTRATION(89,1)\|SPREAD PEAT SOIL(84,4)\|RAINFALL INFILTRATION PERFORMANCE(83,1)\|SOLUTIONTHE INORGANIC CARBON(83,1)\|PERMEABILITY ENHANCEMENT(82,2)\|UNDERGROUND WATERTHE CARBON SEQUESTRATION(76,1)\|LEAD RAINFALL INFILTRATION(67,1)\|PEAT SOIL(63,21)\|PEAT SOIL DRYING(63,6)\|RECYCLING CARBON(60,1)\|RAINFALL(59,12)\|ADSORBABILITY(58,6)\|INFILTRATION(47,6)\|RAINFALL INFILTRATION RECHARGE AREA(47,1)\|GROUNDWATER CARBON SEQUESTRATION(46,1)\|SITE GI ANALYSIS(46,1)\|REPLENISHMENT AREA(44,2)\|TILED PEAT SOIL(43,2)\|FUNCTION MANUAL SPRINKLING(43,1)\|SOIL ADSORPTION(42,2)\|PEAT SOIL WETTING(41,2)\|ATMOSPHERIC RAINFALL(39,3)\|CARBON SEQUESTRATION SIGNIFICANCE(35,2)\|ADSORPTION FUNCTION(35,1)\|SPREADING PEAT SOIL(34,3)\|SPREADING AREA(33,2)\|GROUNDWATER(32,3)\|MODE FUNCTION MANUAL SPRINKLING(32,1)\|DEM THREE DIMENSIONAL MODEL(27,4)\|FLOW CIRCULATION MODE(26,1)\|GROUND SURFACE(25,6)\|CARBON SINK(22,25)\|SPREADING THICKNESS(22,3)\|EFFICIENCY FUNCTION(22,2)\|JIG(21,2)\|CARBON SEQUESTRATION EFFICIENCY FUNCTION(21,1)\|RAINFALL INFILTRATION ELUVIATION(20,1)\|GULLY(19,4)\|RAINFALL INFILTRATION REPLENISHMENT REGION(19,2)\|DISSOLVED INORGANIC CARBON(17,24)\|DEPRESSION(17,4)\|3D MODEL(16,4)\|WATER INFILTRATION(16,3)\|ROTARY TRANSFORMER(16,1)\|RAINFALL INFILTRATION REPLENISHMENT AREA(15,3)\|STORAGE FUNCTION(15,1)\|FIELD GI ANALYSIS(14,3)\|COLLECTION AREA(13,4)\|HCO(13,4)\|RAINFALL SURFACE RUNOFF(12,6)\|FIELD GI(12,3)\|RAINFALL INFILTRATION CHANNEL(12,1)\|RAINFALL INFILTRATION PASSAGE(12,1)\|ADSORPTION PERFORMANCE(10,3)\|RAINFALL INFILTRATION CAPACITY(10,2)\|ECONOMIC PROSPECT(10,1)\|ATMOSPHERIC ABATEMENT(9,1)\|CREATIVE EFFORT(9,1)\|ADSORPTION CAPACITY(8,2)\|CARBON NEUTRALIZATION(8,2)\|DIAMETER FUNCTION(7,4)\|POROSITY(7,3)\|COLLECTION REGION(6,2)\|PERMEABILITY(6,2)\|RETENTION PERFORMANCE(6,2)\|SPRAYING MODE(6,2)\|STAINLESS STEEL ROD(6,2)\|\|(CN114522512)\|CARBON SINK(100,30)\|AQUATIC PHOTOSYNTHESIS(100,12)\|AQUATIC CARBON SINK(100,5)\|AQUATIC ANIMAL(100,2)\|CARBON SINK CAPACITY(100,2)\|DIC FERTILIZATION(69,1)\|AQUATIC CARBON SEQUESTRATION(61,1)\|ATMOSPHERIC CO2IN(51,1)\|AQUATIC CARBON(50,4)\|RAINWATER(49,13)\|GASEOUS FORM2IS(44,3)\|CARBON CIRCULATION(42,1)\|RAIN WATER GUIDE(41,1)\|INORGANIC CARBON(40,11)\|LAND CARBONATE(40,6)\|LAND CARBONATE WEATHERING(38,3)\|SOIL2STORAGE CAPACITY(38,3)\|POPULARIZATION(37,1)\|RAINFALL(35,13)\|SOIL2ENRICHING(35,4)\|RAINFALL INFILTRATION(33,6)\|FIELD2THE PEAT SOIL(32,3)\|AQUATIC PLANT(31,11)\|AQUATIC(29,3)\|ATMOSPHERIC RAINFALL(28,3)\|SOIL PORE(27,8)\|RAINFALL AREA(27,3)\|CARBON SEQUESTRATION(26,5)\|DISSOLVED INORGANIC CARBON(25,25)\|GROUNDWATER(25,9)\|SINK(25,4)\|TERM SCHEMATIC REPRESENTATION(25,1)\|ATMOSPHERE2WITHOUT(23,2)\|NATURAL CONDITION(23,1)\|STABLE ORGANIC CARBON SINK(21,1)\|GROUND LAYER(20,6)\|CARBON SINK SIGNIFICANCE(20,2)\|AQUATIC PHOTOSYNTHETIC ORGANISM PRODUCTIVITY(17,1)\|ORGANIC CARBON SINK(16,2)\|UNDERGROUND WATER(15,4)\|WATERTHE BIOMASS DIC(15,1)\|DREDGE(14,3)\|INORGANIC CARBON VOLUME(14,3)\|PASSAGEWAY(14,3)\|POROSITY(14,3)\|LAYING(14,1)\|ORGANIC CARBON(13,11)\|CARBON SINK FORMATION(13,2)\|WATER BODY(10,20)\|HCO(10,5)\|ATMOSPHERIC CO2THE PATHWAY(10,1)\|UNCHANGING RAINFALL CONDITION PREMISE(10,1)\|PHYTOPLANKTON PRODUCTIVITY(9,1)\|DISSOLVED INORGANIC CARBON CONTENT(8,2)\|DISSOLVED INORGANIC CARBON SOURCE(7,5)\|SURFACE RUNOFF(7,4)\|ATMOSPHERIC CO2STORED(7,1)\|LAND AQUATIC ECOSYSTEM(7,1)\|ATMOSPHERIC CO2AND(6,1)\|CARBON SINK ECONOMIC PROSPECT(6,1)\|CARBONATE WEATHERING CARBON(6,1)\|CREATIVE EFFORT(6,1)\|NATIONAL CARBURANT(6,1)\|RAW MATERIAL(6,1)\|CARBONATE ROCK CONTENT(5,1)\|CO2THE KEY(5,1)\|DIC PROMINENT SOURCE(5,1)\|UNDERGROUND ENVIRONMENT(5,1)\|SURFACE WATER(4,20)\|STEP THREE(4,3)\|PEAT SOIL(4,2)\|CARBON NEUTRALIZATION(4,1)\|CO2THEREFORE(4,1)\|FUNDAMENTAL KEY(4,1)\|LIGHT PARTICIPATION(4,1)\|PHOTOSYNTHESIS2WITH(4,1)\|ALKALINITY(3,1)\|	(CN115445393)\|1. A method for improving the carbon sink efficiency of soil and underground water is characterized by comprising the following steps: the method comprises the following steps:\| Firstly, judging and extracting a main rainfall infiltration supplementing area through site GIS analysis and a DEM three-dimensional model to serve as an area for increasing rainfall infiltration; \| secondly, spreading peat soil with high adsorptivity and high water content to the area selected in the first step, and wetting the dried peat soil with water before spreading; \| thirdly, inserting holes in the peat soil which is well paved, enhancing the permeability of the paved area, and enabling more surface rainfall to enter soil and groundwater space through infiltration so as to increase the CO 2 absorbed by the peat soil; \| And fourthly, increasing the water infiltration amount by adopting a manual sprinkling or leaching mode in a rainfall-free season, increasing the CO 2 amount adsorbed by peat soil, and absorbing and storing atmospheric CO 2 in soil and underground water to form dissolved inorganic carbon so as to realize the purpose of carbon sink. \|2. A method for enhancing the efficiency of carbon sequestration of soil and groundwater according to claim 1, wherein the primary rainfall infiltration replenishment zone in the first step is designated as a rainfall surface runoff collection zone comprising gullies and depressions created by rainfall.\|3. The method for improving the carbon sequestration efficiency of soil and groundwater according to claim 1, wherein the step of spreading peat soil in the second step comprises the steps of: the peat soil with high adsorptivity and high water content is paved in the area selected in the first step, the paving thickness is 5-10cm, the dried peat soil is wetted by water before paving, and the water content of the wetted peat soil is ensured to be 45% -55%.\|4. The method for improving the carbon sequestration efficiency of soil and groundwater according to claim 1, wherein the third step of inserting holes in the tiled peat soil comprises the following steps: the vertical sticks with the diameter of 1cm and the length of 100cm are inserted into the well-paved peat soil, and the density of the formed insertion holes is 10cm multiplied by 10cm, so that more surface rainfall can enter the soil and the groundwater space through infiltration, and the CO 2 absorbed by the peat soil is increased.\|5. The method of claim 1, wherein the dissolved inorganic carbon comprises dissolved CO 2、HCO3- ions and CO 32- ions.	(CN115445393)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of increasing carbon sink and improving carbon circulation, and particularly relates to a method for improving carbon sink efficiency of soil and underground water.\|BACKGROUND ART\|[0002] The aim of China is to realize the aims of carbon reaching peak and carbon neutralization in 2030 and 2060 respectively, and increasing the carbon yield and reducing the carbon emission are the most urgent means for realizing the two aims. However, under the current international economic pressure, the promotion of emission reduction work has certain difficulty in order to ensure good development of economy. Thus, adding carbon sinks or finding new ways of carbon sinks is an important ring to achieve both goals. Carbon sequestration is a mechanism for removing CO 2 from the atmosphere, i.e., absorbing CO 2 from the atmosphere into ecosystems such as land and sea and storing it. Wherein, the soil and the groundwater can form the atmospheric CO 2 into dissolved inorganic carbon (mainly comprising several forms, namely dissolved CO 2(aq)、HCO3- ions and CO 32- ions) through the karst action of rock and the hydrolytic action of CO 2 and water. The part of the formed dissolved inorganic carbon mainly enters soil and underground space through a rainfall infiltration channel under the action of rainfall infiltration flushing and is stored to form a carbon sink process for reducing atmospheric CO 2. In this process, two steps are particularly important, namely, the absorption of CO 2 by the soil, and the surface soil has larger pores and can absorb and store atmospheric CO 2. But the soil has different properties, and the porosity and the adsorption capacity are different; secondly, if CO 2 adsorbed and stored by soil does not enter the deep underground space or enters the dynamic underground water space in time, the CO 2 returns to the atmosphere again, carbon sinks cannot be formed, and the main driving force of the process is leaching effect of rainfall infiltration, namely the amount of the rainfall infiltration into the underground water needs to be increased, so that the amount of the CO 2 entering the deep underground space can be increased more, and more carbon sinks are formed.\|[0003] Therefore, the method for improving the carbon sink efficiency of the soil and the underground water is developed to perfect the engineering technology of carbon sink improvement in China and improve the practical application prospect of the carbon sink.\|DISCLOSURE\|Disclosure of Invention\|[0004] The invention aims to provide a technology for improving carbon sink efficiency of soil and underground water, which is used for improving the carbon sink efficiency of the soil and the underground water for absorbing and storing CO 2 by improving the performance of the soil for absorbing CO 2 and according to the combination form of CO 2 and water in the surface process and the flow circulation mode, and solving the problems in the background technology.\|[0005] In order to solve the technical problems, the invention is realized by the following technical scheme:\|[0006] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps: \|[0007] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; \|[0008] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 45% -55%; \|[0009] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; \|[0010] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. \|[0011] Preferably, the main rainfall infiltration replenishment area in the first step is used as a rainfall surface runoff collection area, and the rainfall surface runoff collection area comprises a gully and a depression formed by rainfall.\|[0012] Preferably, the step of spreading peat soil in the second step specifically includes the following steps: the peat soil with high adsorptivity and high water content is paved in the area selected in the first step, the paving thickness is 5-10cm, the dried peat soil is wetted by water before paving, and the water content of the wetted peat soil is ensured to be 45% -55%.\|[0013] Preferably, the inserting holes on the tiled peat soil in the third step specifically include the following steps: the vertical sticks with the diameter of 1cm and the length of 100cm are inserted into the well-paved peat soil, and the density of the formed insertion holes is 10cm multiplied by 10cm, so that more surface rainfall can enter the soil and the groundwater space through infiltration, and the CO 2 absorbed by the peat soil is increased.\|[0014] Preferably, the dissolved inorganic carbon comprises dissolved CO 2、HCO3- ions and CO 32- ions.\|[0015] Preferably, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other of which is atmospheric CO 2 absorbed by the soil.\|[0016] The invention has the following beneficial effects:\|[0017] According to the invention, the content of dissolved inorganic carbon entering the soil and underground water can be greatly increased through the carrying process of soil adsorption and rainfall infiltration leaching, so that atmospheric CO 2 is stored in a deep underground space, the carbon sink efficiency of the soil and underground water is improved, the method has important carbon sink significance, the efficient removal of CO 2 in the atmosphere can be realized, and the environmental negative effect can not be generated. \|[0018] Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.\|INVENTION MODE\|Detailed Description\|[0019] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.\|[0020] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps:\|[0021] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; \|[0022] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 50%; \|[0023] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; \|[0024] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. \|[0025] According to statistical analysis, the higher the adsorption performance of the soil is, the stronger the adsorption capacity of the soil to atmospheric CO 2 is; in addition, the more rainfall infiltration channels of the soil are, the stronger the rainfall infiltration capacity is, and the more CO 2 is carried by rainfall infiltration, so that the content of dissolved inorganic carbon entering a water body can be effectively increased by 2-3 times by a method of increasing the adsorption quantity of CO 2 in the soil and the rainfall infiltration quantity, and the formed carbon sink quantity is increased by 2-3 times, thereby having important carbon sink economic prospects.\|[0026] In this example, the Dissolved Inorganic Carbon (DIC) includes dissolved CO 2、HCO3- ions and CO 32- ions.\|[0027] In this embodiment, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other is atmospheric CO 2 absorbed by the soil.\|[0028] Increasing the dissolution into the soil and the groundwater is fundamental key to increasing carbon sequestration. While there are two sources of Dissolved Inorganic Carbon (DIC) in soil and groundwater, the highly adsorptive absorption of atmospheric CO 2 by peat soil and the infiltration leaching of atmospheric rainfall carry the absorbed dissolved inorganic carbon. The two parts realize the purposes of reducing, transferring and finally storing the atmospheric CO 2 from the atmosphere into soil and underground water, are the most main CO 2 carbon sink mode, achieve the purpose of increasing carbon sink, and provide technological support for national carburetion sink and realizing important targets of carbon peak and carbon neutralization.\|[0029] In the description of the present specification, the descriptions of the terms "one embodiment," "example," "specific example," and the like, mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.\|[0030] The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof.	(CN115445393)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention belongs to the technical field of increasing carbon sink and improving carbon circulation, and particularly relates to a method for improving carbon sink efficiency of soil and underground water.\|BACKGROUND ART\|[0002] The aim of China is to realize the aims of carbon reaching peak and carbon neutralization in 2030 and 2060 respectively, and increasing the carbon yield and reducing the carbon emission are the most urgent means for realizing the two aims. However, under the current international economic pressure, the promotion of emission reduction work has certain difficulty in order to ensure good development of economy. Thus, adding carbon sinks or finding new ways of carbon sinks is an important ring to achieve both goals. Carbon sequestration is a mechanism for removing CO 2 from the atmosphere, i.e., absorbing CO 2 from the atmosphere into ecosystems such as land and sea and storing it. Wherein, the soil and the groundwater can form the atmospheric CO 2 into dissolved inorganic carbon (mainly comprising several forms, namely dissolved CO 2(aq)、HCO3- ions and CO 32- ions) through the karst action of rock and the hydrolytic action of CO 2 and water. The part of the formed dissolved inorganic carbon mainly enters soil and underground space through a rainfall infiltration channel under the action of rainfall infiltration flushing and is stored to form a carbon sink process for reducing atmospheric CO 2. In this process, two steps are particularly important, namely, the absorption of CO 2 by the soil, and the surface soil has larger pores and can absorb and store atmospheric CO 2. But the soil has different properties, and the porosity and the adsorption capacity are different; secondly, if CO 2 adsorbed and stored by soil does not enter the deep underground space or enters the dynamic underground water space in time, the CO 2 returns to the atmosphere again, carbon sinks cannot be formed, and the main driving force of the process is leaching effect of rainfall infiltration, namely the amount of the rainfall infiltration into the underground water needs to be increased, so that the amount of the CO 2 entering the deep underground space can be increased more, and more carbon sinks are formed.\|[0003] Therefore, the method for improving the carbon sink efficiency of the soil and the underground water is developed to perfect the engineering technology of carbon sink improvement in China and improve the practical application prospect of the carbon sink.\|DISCLOSURE\|Disclosure of Invention\|[0004] The invention aims to provide a technology for improving carbon sink efficiency of soil and underground water, which is used for improving the carbon sink efficiency of the soil and the underground water for absorbing and storing CO 2 by improving the performance of the soil for absorbing CO 2 and according to the combination form of CO 2 and water in the surface process and the flow circulation mode, and solving the problems in the background technology.\|[0005] In order to solve the technical problems, the invention is realized by the following technical scheme:\|[0006] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps: \|[0007] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; \|[0008] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 45% -55%; \|[0009] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; \|[0010] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. \|[0011] Preferably, the main rainfall infiltration replenishment area in the first step is used as a rainfall surface runoff collection area, and the rainfall surface runoff collection area comprises a gully and a depression formed by rainfall.\|[0012] Preferably, the step of spreading peat soil in the second step specifically includes the following steps: the peat soil with high adsorptivity and high water content is paved in the area selected in the first step, the paving thickness is 5-10cm, the dried peat soil is wetted by water before paving, and the water content of the wetted peat soil is ensured to be 45% -55%.\|[0013] Preferably, the inserting holes on the tiled peat soil in the third step specifically include the following steps: the vertical sticks with the diameter of 1cm and the length of 100cm are inserted into the well-paved peat soil, and the density of the formed insertion holes is 10cm multiplied by 10cm, so that more surface rainfall can enter the soil and the groundwater space through infiltration, and the CO 2 absorbed by the peat soil is increased.\|[0014] Preferably, the dissolved inorganic carbon comprises dissolved CO 2、HCO3- ions and CO 32- ions.\|[0015] Preferably, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other of which is atmospheric CO 2 absorbed by the soil.\|[0016] The invention has the following beneficial effects:\|[0017] According to the invention, the content of dissolved inorganic carbon entering the soil and underground water can be greatly increased through the carrying process of soil adsorption and rainfall infiltration leaching, so that atmospheric CO 2 is stored in a deep underground space, the carbon sink efficiency of the soil and underground water is improved, the method has important carbon sink significance, the efficient removal of CO 2 in the atmosphere can be realized, and the environmental negative effect can not be generated. \|[0018] Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.\|INVENTION MODE\|Detailed Description\|[0019] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.\|[0020] The invention relates to a method for improving the carbon sink efficiency of soil and underground water, which comprises the following steps:\|[0021] Firstly, judging and extracting a main rainfall infiltration supply area through site GIS analysis and a DEM three-dimensional model, wherein the main rainfall infiltration supply area comprises rainfall surface runoff collection areas such as ditches and depressions formed after rainfall in the area, and the rainfall surface runoff collection areas are used as areas for increasing rainfall infiltration quantity; \|[0022] The second step, peat soil has huge water absorption and water retention properties, high porosity and strong adsorption performance, and is a very good soil improvement material, so the peat soil is relatively suitable for being used as a soil physical modifier. Spreading peat soil with high adsorptivity and high water content to the first selected area with a spreading thickness of 5-10cm, wetting the dried peat soil with water before spreading, and ensuring water content to be 50%; \|[0023] thirdly, stainless steel vertical sticks with the diameter of 1cm and the length of 100cm are adopted, and density jacks with the density of 10cm multiplied by 10cm are arranged in a region where peat soil is paved, so that the permeability of the paved region is enhanced, more surface rainfall can enter soil and underground water space through infiltration, and the CO 2 absorbed by peat soil is increased; \|[0024] And fourthly, in the rainfall-free season, the water infiltration amount is increased by adopting a manual sprinkling mode, and the CO 2 amount adsorbed by peat soil is increased by adopting a leaching mode, so that the purposes of absorbing and storing atmospheric CO 2 in soil and groundwater to form dissolved inorganic carbon and further realizing carbon sink are achieved. \|[0025] According to statistical analysis, the higher the adsorption performance of the soil is, the stronger the adsorption capacity of the soil to atmospheric CO 2 is; in addition, the more rainfall infiltration channels of the soil are, the stronger the rainfall infiltration capacity is, and the more CO 2 is carried by rainfall infiltration, so that the content of dissolved inorganic carbon entering a water body can be effectively increased by 2-3 times by a method of increasing the adsorption quantity of CO 2 in the soil and the rainfall infiltration quantity, and the formed carbon sink quantity is increased by 2-3 times, thereby having important carbon sink economic prospects.\|[0026] In this example, the Dissolved Inorganic Carbon (DIC) includes dissolved CO 2、HCO3- ions and CO 32- ions.\|[0027] In this embodiment, the surface water has two sources of dissolved inorganic carbon, one of which is dissolved inorganic carbon in the atmospheric precipitation, and the other is atmospheric CO 2 absorbed by the soil.\|[0028] Increasing the dissolution into the soil and the groundwater is fundamental key to increasing carbon sequestration. While there are two sources of Dissolved Inorganic Carbon (DIC) in soil and groundwater, the highly adsorptive absorption of atmospheric CO 2 by peat soil and the infiltration leaching of atmospheric rainfall carry the absorbed dissolved inorganic carbon. The two parts realize the purposes of reducing, transferring and finally storing the atmospheric CO 2 from the atmosphere into soil and underground water, are the most main CO 2 carbon sink mode, achieve the purpose of increasing carbon sink, and provide technological support for national carburetion sink and realizing important targets of carbon peak and carbon neutralization.\|[0029] In the description of the present specification, the descriptions of the terms "one embodiment," "example," "specific example," and the like, mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.\|[0030] The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof.	Family Number\|(100174807)\|100174807\|Object of Invention\|(CN114522512 A)\|The invention discloses a method for increasing aquatic carbon sequestration , and relates to the technical field of carbon sequestration increasing and carbon circulation improving . \|(CN115445393 A)\|( . . . ) circulation mode of the system and water in the earth surface process realize the increase of the absorption and storage of CO in soil and underground water by improving the rainfall infiltration performance of an earth surface system 2 The carbon sequestration efficiency of ( 2 ) solves the problems in the background art . \|The invention discloses a method for improving carbon sequestration efficiency of soil and underground water , and relates to the technical field of carbon sequestration increasing and carbon recycling improving . \|Abstract\|(CN114522512 A)\|The invention discloses a method for increasing the carbon sink amount of aquatic products , and relates to the technical field of carbon sink increasing and carbon cycle improving . The method comprises the following steps : step 1, absorbing atmospheric CO2 in a carbonate rock weathering process , so that CO2 is temporarily captured and stored in soil pores , and enrichment of CO2 in soil is realized ; step 2, by guiding rainwater in the field area during rainfall , rainwater carrying dissolved inorganic carbon is increased to infiltrate into underground water and flows into a surface water body through surface runoff , and the amount of the dissolved inorganic carbon in the surface water body is increased ; and 3, converting dissolved inorganic carbon in the water body into organic carbon through photosynthesis of the aquatic plants , and storing the organic carbon , so that the aquatic carbon sink in the water body is realized . According to the method , the content of dissolved inorganic carbon entering a surface water body can be greatly increased , so that the fertilization effect is improved , the amount of carbon sink formed by aquatic photosynthesis is increased , the method has important carbon sink significance , CO2 in the atmosphere can be efficiently removed , and the environmental negative effect cannot be generated . \|(CN115445393B B)\|The invention discloses a method for improving the carbon sink efficiency of soil and underground water , and relates to the technical field of carbon sink increase and carbon cycle improvement . The method comprises the following steps : step 1, judging and extracting a main rainfall infiltration supply area through site GIS analysis and DEM three - dimensional model , and taking the main rainfall infiltration supply area as an area for increasing the rainfall infiltration amount ; step 2, paving peat soil with a high - adsorbability and high - water - content space to the area selected in the step 1, and wetting the dried peat soil with water before paving ; thirdly , holes are formed in the laid peat soil , the permeability of a laid area is enhanced , more earth surface rainfall can enter the soil and underground water space through infiltration , and the CO2 amount adsorbed by the peat soil is increased . Through soil adsorption and rainfall infiltration leaching carrying processes , the content of dissolved inorganic carbon entering the soil and underground water is greatly increased , so that atmospheric CO2 is stored in a deep underground space , the carbon sequestration efficiency of the soil and underground water is improved , and important carbon sequestration significance is achieved . \|Independent Claims\|(CN114522512 A)\|( . . . ) step two , controlling the rainfall infiltration process : in the first step , inorganic carbon captured and stored in soil pores is mixed with rainwater in the rainfall process to form dissolved inorganic carbon , rainwater carrying the dissolved inorganic carbon is increased to infiltrate into underground water through guiding the rainwater in ( . . . ) \|(CN115445393 A)\|1. A method for improving carbon sequestration efficiency of soil and underground water is characterized by comprising the following steps : the method comprises the following steps : ( . . . ) \|	Environmental technology	B01D-053/14/75\|C02F-003/32\|C02F-2101/10\|C02F-2103/001\|Y02P-060/20		B01D-053/14/75\|C02F-003/32\|C02F-2101/10\|C02F-2103/001\|Y02P-060/20	B01D-053/14\|C02F-003/32	B01D-053/14\|C02F-003/32			CN119028214\|CN117069270	CN119028214 112341928 WHO=Examiner SELF=N CAT=A\|CN117069270 107332388 WHO=Examiner SELF=N CAT=A	AU2020202329\|CN106577116\|CN105130001\|CN102577688	AU2020202329 91096696 WHO=Examiner SELF=N\|CN106577116 75959932 WHO=Examiner SELF=N\|CN105130001 71632395 WHO=Examiner SELF=N\|CN102577688 7762768 WHO=Examiner SELF=N		AU2020202329; CN102577688; CN105130001; CN106577116\|		GRANTED	(CN115445393)\|GRANTED\|(CN114522512)\|LAPSED	ALIVE	(CN115445393)\|ALIVE\|(CN114522512)\|DEAD	(CN115445393)\|LEGAL DETAILS FOR CN115445393\|Actual or expected expiration date=2042-10-26\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2022-10-26\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202211317927\|Application date=2022-10-26\|Standardized application number=2022CN-1317927\|Event publication date=2022-12-09\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN115445393\|Publication stage code=A\|Publication date=2022-12-09\|Standardized publication number=CN115445393\|Event publication date=2022-12-09\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2022-12-27\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2024-04-26\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN115445393\|Publication stage code=B\|Publication date=2024-04-26\|Standardized publication number=CN115445393B\|Event publication date=2024-04-26\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|(CN114522512)\|LEGAL DETAILS FOR CN114522512\|Actual or expected expiration date=2022-12-06\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-01-21\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202210073314\|Application date=2022-01-21\|Standardized application number=2022CN-0073314\|Event publication date=2022-05-24\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN114522512\|Publication stage code=A\|Publication date=2022-05-24\|Standardized publication number=CN114522512\|Event publication date=2022-05-24\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2022-06-10\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2022-12-06\|Event code=CN/WD01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent application deemed withdrawn after publication		(CN115445393)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTeP+miV6FakRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1		https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=KsolU%252FVsjE2he6%252Fe1BZ8qLmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN115445393)\|CN\|(CN115445393)\|CN\|(CN114522512)\|CN	(CN115445393)\|NAME=GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY , COUNTRY=CN\|(CN115445393)\|NAME=GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY , COUNTRY=CN\|(CN114522512)\|NAME=GUIZHOU TIANWING CONSTANT FULL MINERAL RESOURCE ENGINEERING DESIGN LTD COMPANY , COUNTRY=CN		(CN115445393)\|NAME=CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP) , REG=11308\|(CN115445393)\|NAME=CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP) , REG=11308\|(CN114522512)\|NAME=CAO GUANGSHENG;BEIJING YUANBEN INTELLECTUAL PROPERTY LAW OFFICE (GENERAL PARTNERSHIP) , REG=11308	\|(CN115445393)\|CN\|(CN114522512)\|CN	(CN115445393)\|NAME=YANG MINGXING\|NAME=ZHANG MIN\|NAME=YANG WU\|NAME=XIE FEI\|NAME=YAO DUNTING\|NAME=LI WEI\|(CN115445393)\|NAME=YANG MINGXING, COUNTRY=CN \|NAME=ZHANG MIN\|NAME=YANG WU\|NAME=XIE FEI\|NAME=YAO DUNTING\|NAME=LI WEI\|(CN114522512)\|NAME=YANG MINGXING, COUNTRY=CN \|NAME=ZHANG MIN\|NAME=YANG WU\|NAME=XIE FEI		1	2					(CN115445393)\|Number of Claims: NCL=5\|Gazette date: GAZDATE=2024-04-26\|Gazette number: GAZNUM=40-1702\|Number of Pages: NPAGES=5\|Primary examiner: 孙黎\|Primary examiner: Sun Li\|\|(CN115445393)\|Number of Claims: NCL=6\|Gazette date: GAZDATE=2022-12-09\|Gazette number: GAZNUM=38-4902\|Substantial examination effective date: 20221227 Examination duration: 15 months\|Number of Pages: NPAGES=5\|Primary examiner: 孙黎\|Primary examiner: Sun Li\|\|(CN114522512)\|Number of Claims: NCL=5\|Gazette date: GAZDATE=2022-05-24\|Gazette number: GAZNUM=38-2101\|Substantial examination effective date: 20220610\|Number of Pages: NPAGES=5\|	(CN115445393)\|Previous publication: CN115445393 A 2022-12-09 [CN115445393]	(CN115445393)\|CHINESE (CHI)	(CN115445393B)\|Patent\|(CN115445393)\|Patent\|(CN114522512)\|Patent	Titre: (CN115445393)\|Method for improving carbon sink efficiency of soil and underground water Résumé: (CN115445393)\|The invention discloses a method for improving the carbon sink efficiency of soil and underground water, and relates to the technical field of carbon sink increase and carbon cycle improvement. The method comprises the following steps: step 1, judging and extracting a main rainfall infiltration supply area through site GIS analysis and DEM three-dimensional model, and taking the main rainfall infiltration supply area as an area for increasing the rainfall infiltration amount; step 2, paving peat soil with a high-adsorbability and high-water-content space to the area selected in the step 1, and wetting the dried peat soil with water before paving; thirdly, holes are formed in the laid peat soil, the permeability of a laid area is enhanced, more earth surface rainfall can enter the soil and underground water space through infiltration, and the CO2 amount adsorbed by the peat soil is increased. Through soil adsorption and rainfall infiltration leaching carrying processes, the content of dissolved inorganic carbon entering the soil and underground water is greatly increased, so that atmospheric CO2 is stored in a deep underground space, the carbon sequestration efficiency of the soil and underground water is improved, and important carbon sequestration significance is achieved.	20	Abstract	gpt-4o-mini	no	The method focuses on improving carbon sink efficiency through soil and water management rather than accelerating mineral weathering or CO2 capture via mineral carbonation.
22	GB201306559\|GB201406520\|WOEP2015/025018	WOEP2015/025018\|EP15723131\|ES15723131T\|DK15723131T\|CN201580030663\|US15/303,208\|GB201406520\|GB201306559	ES2824676\|DK3129125\|EP3129125\|CN106573197\|US9963351\|CN106573197\|EP3129125\|US20170029284\|GB2516141\|WO2015/154887\|GB2515995\|GB2516141\|GB201406520\|GB201306559	45351908	WO2015/154887 A1 2015-10-15 [WO2015154887]\|EP3129125 B1 2020-07-15 [EP3129125]\|EP3129125 A1 2017-02-15 [EP3129125]\|ES2824676 T3 2021-05-13 [ES2824676]\|DK3129125 T3 2020-10-19 [DK3129125T]\|CN106573197 B 2019-08-23 [CN106573197B]\|CN106573197 A 2017-04-19 [CN106573197]\|US9963351 B2 2018-05-08 [US9963351]\|US20170029284 A1 2017-02-02 [US20170029284]\|GB2516141 B 2016-10-05 [GB2516141]\|GB2516141 A 2015-01-14 [GB2516141]\|GB201406520 D0 2014-05-28 [GB201406520]\|GB2515995 A 2015-01-14 [GB2515995]\|GB201306559 D0 2013-05-22 [GB201306559]	2013-04-10\|2014-04-10\|2015-04-10	2015-04-10\|2015-04-10\|2015-04-10\|2015-04-10\|2015-04-10\|2015-04-10\|2014-04-10\|2013-04-10	2021-05-13\|2020-10-19\|2020-07-15\|2019-08-23\|2018-05-08\|2017-04-19\|2017-02-15\|2017-02-02\|2016-10-05\|2015-10-15\|2015-01-14\|2015-01-14\|2014-05-28\|2013-05-22	(EP3129125)\|2020-07-15\|(US9963351)\|2018-05-08\|\|(GB2516141)\|2016-10-05\|\|(CN106573197B)\|2019-08-23\|(ES2824676)\|2021-05-13\|(DK3129125T)\|2020-10-19	(EP3129125)\|2035-04-10\|(US9963351)\|2035-07-11\|(WO2015/154887)\|2017-10-10\|(GB2516141)\|2024-04-10\|(GB2515995)\|2018-02-21\|(CN106573197)\|2035-04-10\|(ES2824676)\|2035-04-10\|(DK3129125)\|2024-04-30	(EP3129125)\|Method of activation of mineral silicate minerals	(EP3129125)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.	CAMBRIDGE CARBON CAPTURE	(EP3129125)\|Cambridge Carbon Capture Ltd. ([GB])\|(EP3129125)\|Cambridge Carbon Capture Ltd. ([GB])\|(US9963351)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(US20170029284)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(WO2015/154887)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(GB2516141)\|Cambridge Carbon Capture Ltd\|(GB2516141)\|CAMBRIDGE CARBON CAPTURE LTD\|(GB201406520)\|CAMBRIDGE CARBON CAPTURE LTD\|(GB2515995)\|CAMBRIDGE CARBON CAPTURE LTD\|(GB201306559)\|CAMBRIDGE CARBON CAPTURE LTD\|(CN106573197)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(CN106573197)\|CAMBRIDGE CARBON CAPTURE LTD ([GB])\|(ES2824676)\|Cambridge Carbon Capture Ltd.\|(DK3129125)\|Cambridge Carbon Capture Ltd.	PRIESTNALL MICHAEL	(EP3129125)\|PRIESTNALL, Michael\|(EP3129125)\|PRIESTNALL, Michael	(EP3129125)\|Norris, Timothy Sweyn;Basck ([GB])\|Reg. Nb: 101324986\|(WO2015/154887)\|NORRIS, Timothy Sweyn ([GB])\|(CN106573197)\|ZHU HAIYAN;TAHOTA LAW FIRM\|Reg. Nb: 51219	(EP3129125)\|Additional aspects, advantages, features and objects of the present invention would be made apparent from the drawings and the detailed description of the illustrative embodiments construed in conjunction with the appended claims that follow. It will be appreciated that features of the present invention are susceptible to being combined in various combinations from different embodiments without departing from the scope of the present invention as defined by the appended claims.\|From the graph, it will be appreciated that the proportion of Dunite, namely magnesium silicate, converted to Brucite, namely magnesium hydroxide, increases approximately linearly with increase in NaOH concentration; extrapolation of this graph indicates that the proportion of Brucite in the solid product should approach 100% above a NaOH concentration >70mol/kg, namely equivalent to a NaOH: H2O ratio >1.26; FIG. 6 is an illustration of XRD patterns of solid products from dissolution of Dunite at 180 °C with Sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg solution, for different temporal durations; FIG. 7a and 7b are illustrations of TG (7a) and DTG (7b) curves of solid products from dissolution of Dunite at a temperature of 180° C with sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg for different temporal durations; FIG. 8 is a graph in which there is shown Magnesium Hydroxide Mg(OH)2 concentration in solid products based on TG results: Dunite dissolved at a temperature of 180 °C with a molar concentration of Sodium Hydroxide (NaOH) solution being 40 mol/kg for different durations; FIG. 9 is an illustration showing Rietveld Refinement QPA of raw Dunite, wherein: data points profile = experimental pattern; continue profile = calculated model (above); difference plot (below); FIG. 10 is an illustration showing Rietveld Refinement QPA of dissolved Dunite spiked with 10 wt% Silicon, wherein: data points profile = experimental pattern; continue profile = calculated model; and FIG. 11a and 11b are illustrations showing Brucite quantification with Rietveld Refinement and TGA ( FIG. 11a ), wherein Forsterite and Brucite concentrations were obtained via Rietveld Refinement QPA of selected samples ( FIG. 11b ).\|The current invention allows for the method and system to operate without expensive and complicated equipment used in Blencoe to operate at higher than atmospheric pressure.\|Experiments to determine the kinetics of these reactions (5) and (6) have shown that such reactions also suffer from poor energy efficiency and a high cost when up-scaled to an industrial plant.\|However, the efforts suffer from various limitations, such as energy wastage and a high cost of mining and transporting large amounts of rock, as well as industrial and environmental inefficiencies.\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for removal and Capture of Carbon Dioxide from Flue Gases". Although, the prior art disclosures have been able to address some of the problems of mineral Carbonation through their indirect sequestration processes, there are several remaining problems which have not yet been resolved.\|	(EP3129125)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from the group consisting of alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300 °C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|	(EP3129125)\|The present disclosure relates to methods of producing activated mineral silicate for use in sequestrating Carbon Dioxide, for example from flue-gas, by utilizing a process which involves digestion of metal mineral Silicates. Moreover, the present disclosure also relates to systems for executing aforesaid methods.\|The present invention provides a method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, wherein the method comprises: a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from a group comprising alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300°C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|The present invention seeks to provide an improved method of activation of magnesium silicate minerals by conversion to magnesium hydroxide.\|	(EP3129125)\|MAGNESIA(100,30)\|MAGNESIUM SILICATE(100,28)\|MAGNESIUM SILICATE MINERAL(100,12)\|ACTIVATION(100,3)\|MINERAL SILICATE MINERAL ACTIVATION(100,1)\|UNPRESSURIZED VESSEL(84,5)\|BRUCITE QUANTIFICATION(73,1)\|DRY POWDER(67,4)\|RIETVELD REFINEMENT(60,6)\|TEMPORAL DURATION(60,4)\|INEFFICIENCY(60,2)\|MAGNESIUM SILICATE DRY POWDER(60,2)\|BRUCITE PROPORTION(60,1)\|ALKALINE AQUEOUS LIQUID SLURRY(54,2)\|EXPERIMENTAL PATTERN(49,2)\|DISSOLUTION(46,8)\|SHELL INTERNATIONAL(45,1)\|MODEL CALCULATION(42,2)\|MINERAL CARBONATION(41,5)\|MOLAR RATIO(41,4)\|ENERGY WASTAGE(38,1)\|INDIRECT SEQUESTRATION(35,1)\|METAL MINERAL SILICATE DIGESTION(35,1)\|EQUIPMENT COMPLICATION(33,1)\|EXPENSIVE EQUIPMENT(33,1)\|METHANEDIONE(31,30)\|BICARBONATE(31,5)\|DIFFERENCE PLOT(31,1)\|ROCK(31,1)\|XRD PATTERN(30,2)\|ALKALI METAL SILICATE(28,3)\|BRUCITE(27,22)\|MOLAR CONCENTRATION(27,5)\|H2O RATIO(27,1)\|SODIUM HYDROXIDE(26,60)\|AQUEOUS SOLUTION(26,12)\|SOLID PRODUCT(26,8)\|METHANEDIONE SEQUESTRATION(25,5)\|SOLID GLASS PRODUCT(25,4)\|SOLID PRODUCT XRD PATTERN(23,1)\|GLASS PRODUCT(22,4)\|FORSTERITE(22,3)\|METALLIC MINERAL SILICATE(22,1)\|AQUEOUS PHASE PRODUCTION(21,2)\|SEQUESTRATION METHANEDIONE NONINVENTIVE(21,1)\|SODIUM HYDROXIDE MOLAR CONCENTRATION(21,1)\|ALKALI METAL HYDROXIDE(20,7)\|INDUSTRIAL PLANT(20,1)\|MINERAL SILICATE(19,2)\|SODIUM CARBONATE(17,4)\|ALKALI METAL(16,16)\|DTG(16,2)\|SUSPENDED BRUCITE PARTICLE(15,3)\|SEQUESTRATING METHANEDIONE(15,2)\|FORSTERITE CAREFUL QUANTIFICATION(15,1)\|SERPENTINE FEEDSTOCK TONNE(15,1)\|FLUE GAS(14,14)\|ENERGY EFFICIENCY(12,1)\|SALABLE INDUSTRIAL FEEDSTOCK(12,1)\|ATMOSPHERIC PRESSURE(11,8)\|CO2 SCRUBBING(11,2)\|BRUCITE CARBONATION(11,1)\|CONTEMPORARY RESEARCH OVERVIEW(11,1)\|MAGNESIA TONNE(11,1)\|METHANEDIONE TONNE(11,1)\|MINERAL CARBONATION SCIENCE(11,1)\|OLIVINE CARBONATION(11,1)\|DATA POINT PROFILE(10,2)\|DGC REACTOR(10,2)\|BLENCOE ASSERTION(10,1)\|RIETVELD REFINEMENT QPA(10,1)\|SATISFACTORY MINERAL CARBONATION(10,1)\|SERPENTINE DEHYDROXYLATION(10,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(10,1)\|ALKALI METAL COMPOUND(9,9)\|BICARBONATE ION(9,3)\|CO2 REMOVAL(8,4)\|OLIVINE POWDER(8,2)\|ANTHROPOGENIC OXIDATION(8,1)\|CARBONATION REACTOR(8,1)\|INTENSE PREPROCESSING(8,1)\|MAGNESIA DISSOLVE(8,1)\|MAGNESIA POWDER SUSPENSION(8,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(8,1)\|MINERAL CARBONATION REACTION(8,1)\|MINERAL SEQUESTRATION(8,1)\|NONINVENTIVE EXPERIMENT(8,1)\|OLIVINE DIGESTION(8,1)\|SCALABILITY EXPERIMENT(8,1)\|DATA POINT(7,2)\|INORGANIC POWDER(7,2)\|MAGNESIUM SILICATE CONVERSION(7,2)\|MG3SI2O(7,2)\|STEP CONDITION(7,2)\|BRUCITE SOLUBILITY(7,1)\|CARBONACEOUS FOSSIL FUEL(7,1)\|CO2 DISSOLUTION(7,1)\|CO2 TONNE(7,1)\|ELEMENTAL CONSTITUENT(7,1)\|HUGE ENERGY PENALTY(7,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(7,1)\|MASTER THESIS(7,1)\|MINERAL DIGESTION(7,1)\|MINERALOGICAL SITE(7,1)\|MINING HIGH COST(7,1)\|OLIVINE CONVERSION(7,1)\|OVERNIGHT SHUTDOWN(7,1)\|UTILIZATION OPTION(7,1)\|VESSEL PRESSURIZATION(7,1)\|WOLLASTONITE(6,3)\|ROTAMETER(6,2)\|ALKALINE REAGENT(6,1)\|AQUEOUS MAGNESIA(6,1)\|BRUCITE CONVERSION(6,1)\|BRUCITE MINOR PHASE(6,1)\|BRUCITE POWDER(6,1)\|CO2 METER(6,1)\|CO2 TRANSPORT(6,1)\|CYLINDER PREMIX(6,1)\|DIGESTION VESSEL(6,1)\|DUNITE POWDER(6,1)\|INLET CO2(6,1)\|MAGNESIA YIELD(6,1)\|MAGNESIUM ION(6,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(6,1)\|MAGNESIUM SILICATE MINERAL POWDER(6,1)\|METAL SILICATE CARBONATION(6,1)\|MINERAL HYDROXIDE(6,1)\|MOLE RATION(6,1)\|OCCASIONAL MEASUREMENT(6,1)\|PARTICLE ATTRITION(6,1)\|PREMIX CYLINDER(6,1)\|PRESSURIZATION DEPRESSURIZATION(6,1)\|SAMPLE XRD PATTERN(6,1)\|SLURRY CIRCULATION(6,1)\|SLURRY DROPLET SOLUTION(6,1)\|STABLE MINERAL CARBONATE(6,1)\|STOICHIOMETRIC CONVERSION(6,1)\|VALUABLE MINERAL(6,1)\|AMBIENT ATMOSPHERIC PRESSURE(5,4)\|ALKALINE EARTH SILICATE(5,3)\|CAUSTIC ALKALI METAL HYDROXIDE(5,2)\|HIGH COST(5,2)\|MG2SIO(5,2)\|PRODUCTION THROUGHPUT(5,2)\|SEAWATER(5,2)\|ABUNDANT SOURCE(5,1)\|ACIDIC PRETREATMENT(5,1)\|AGEING(5,1)\|ALKALI TREATMENT(5,1)\|ALKALINE PH(5,1)\|AMBIENT ATMOSPHERE(5,1)\|BLEND CONTENT(5,1)\|BRUCITE MAJOR PHASE(5,1)\|BUBBLE COLUMN(5,1)\|CALCIUM SILICATE MINERAL(5,1)\|CALIBRATED GLASS TUBE ROTAMMETER(5,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(5,1)\|CO2 EMISSION DISTANT SOURCE(5,1)\|CO2 SEQUESTRATION CAPACITY(5,1)\|CONTRADISTINCTION(5,1)\|DOMINANT REACTION(5,1)\|DRY STOICHIOMETRIC REACTION(5,1)\|EARTH ATMOSPHERE(5,1)\|ELECTRICITY GENERATING FACILITY(5,1)\|FEED MINERAL(5,1)\|GEOLOGIC TIMESCALE(5,1)\|GLASS SOLIDIFICATION(5,1)\|HUGE SCALE(5,1)\|HYDROTHERMAL REACTION SAVE(5,1)\|INFRARED DATA LOGGER(5,1)\|INLET GAS CO2(5,1)\|INORGANIC PARTICLE(5,1)\|MAGNESIA PRODUCTION(5,1)\|MAGNESIUM BICARBONATE MG(5,1)\|MAGNESIUM SILICATE CRYSTAL(5,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(5,1)\|MAGNESIUM SILICATE PARTICLE(5,1)\|MAGNESIUM SILICATE POWDER(5,1)\|METHANEDIONE SOURCE(5,1)\|MONITORED EXIT GAS(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONEXCLUSIVE(5,1)\|OLIVINE REACTION(5,1)\|PRECAPTURE(5,1)\|PRIMARY INITIATIVE(5,1)\|QUANTITATIVE PHASE ANALYSIS(5,1)\|REACTION ACCELERATOR(5,1)\|RELIANCE(5,1)\|SALABLE CHEMICAL(5,1)\|SEALED VESSEL(5,1)\|SODIUM HYDROXIDE REGENERATION(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|UNPRESSURIZED CONTINUOUS MODE(5,1)\|UNPRESSURIZED REACTION VESSEL(5,1)\|REACTION PRODUCT(4,6)\|HCO(4,3)\|NONUNDERLINED NUMBER(4,3)\|TEMPERATURE ELEVATION(4,3)\|UNDERLINED NUMERAL(4,3)\|2H2O(4,2)\|STOICHIOMETRIC RATIO(3,4)\|ABSOLUTE UNCERTAINTY(3,1)\|ALKALI DIGESTION(3,1)\|ALKALINE COMPOUND INPUT(3,1)\|ALKALINE SOLUTION(3,1)\|ANTIGORITE(3,1)\|AQUEOUS PHASE CARBONATION(3,1)\|AQUEOUS REACTION(3,1)\|AUTOCLAVE(3,1)\|BOUND HYDROXIDE GROUP(3,1)\|CARBONATION DETAIL(3,1)\|CHRYSOTILE(3,1)\|CLEAR BENEFIT(3,1)\|CO2 CONCENTRATION CHANGE(3,1)\|CO2 DEPLETED GAS(3,1)\|CO2 MASS(3,1)\|COMPACTION(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CONCERN CAUSE(3,1)\|CONTAMINATION(3,1)\|DISCOVERY(3,1)\|DISSOLUTION DISINTEGRATION(3,1)\|ECONOMIC FEASIBILITY(3,1)\|EXCESS ALKALI(3,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(3,1)\|\|(EP3129125)\|MAGNESIA(100,30)\|MAGNESIUM SILICATE(100,28)\|MAGNESIUM SILICATE MINERAL(100,12)\|ACTIVATION(100,3)\|MINERAL SILICATE MINERAL ACTIVATION(100,1)\|UNPRESSURIZED VESSEL(84,5)\|BRUCITE QUANTIFICATION(73,1)\|DRY POWDER(67,4)\|RIETVELD REFINEMENT(60,6)\|TEMPORAL DURATION(60,4)\|INEFFICIENCY(60,2)\|MAGNESIUM SILICATE DRY POWDER(60,2)\|BRUCITE PROPORTION(60,1)\|ALKALINE AQUEOUS LIQUID SLURRY(54,2)\|EXPERIMENTAL PATTERN(49,2)\|DISSOLUTION(46,8)\|SHELL INTERNATIONAL(45,1)\|MODEL CALCULATION(42,2)\|MINERAL CARBONATION(41,5)\|MOLAR RATIO(41,4)\|ENERGY WASTAGE(38,1)\|INDIRECT SEQUESTRATION(35,1)\|METAL MINERAL SILICATE DIGESTION(35,1)\|EQUIPMENT COMPLICATION(33,1)\|EXPENSIVE EQUIPMENT(33,1)\|METHANEDIONE(31,30)\|BICARBONATE(31,5)\|DIFFERENCE PLOT(31,1)\|ROCK(31,1)\|XRD PATTERN(30,2)\|ALKALI METAL SILICATE(28,3)\|BRUCITE(27,22)\|MOLAR CONCENTRATION(27,5)\|H2O RATIO(27,1)\|SODIUM HYDROXIDE(26,60)\|AQUEOUS SOLUTION(26,12)\|SOLID PRODUCT(26,8)\|METHANEDIONE SEQUESTRATION(25,5)\|SOLID GLASS PRODUCT(25,4)\|SOLID PRODUCT XRD PATTERN(23,1)\|GLASS PRODUCT(22,4)\|FORSTERITE(22,3)\|METALLIC MINERAL SILICATE(22,1)\|AQUEOUS PHASE PRODUCTION(21,2)\|SEQUESTRATION METHANEDIONE NONINVENTIVE(21,1)\|SODIUM HYDROXIDE MOLAR CONCENTRATION(21,1)\|ALKALI METAL HYDROXIDE(20,7)\|INDUSTRIAL PLANT(20,1)\|MINERAL SILICATE(19,2)\|SODIUM CARBONATE(17,4)\|ALKALI METAL(16,16)\|DTG(16,2)\|SUSPENDED BRUCITE PARTICLE(15,3)\|SEQUESTRATING METHANEDIONE(15,2)\|FORSTERITE CAREFUL QUANTIFICATION(15,1)\|SERPENTINE FEEDSTOCK TONNE(15,1)\|FLUE GAS(14,14)\|ENERGY EFFICIENCY(12,1)\|SALABLE INDUSTRIAL FEEDSTOCK(12,1)\|ATMOSPHERIC PRESSURE(11,8)\|CO2 SCRUBBING(11,2)\|BRUCITE CARBONATION(11,1)\|CONTEMPORARY RESEARCH OVERVIEW(11,1)\|MAGNESIA TONNE(11,1)\|METHANEDIONE TONNE(11,1)\|MINERAL CARBONATION SCIENCE(11,1)\|OLIVINE CARBONATION(11,1)\|DATA POINT PROFILE(10,2)\|DGC REACTOR(10,2)\|BLENCOE ASSERTION(10,1)\|RIETVELD REFINEMENT QPA(10,1)\|SATISFACTORY MINERAL CARBONATION(10,1)\|SERPENTINE DEHYDROXYLATION(10,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(10,1)\|ALKALI METAL COMPOUND(9,9)\|BICARBONATE ION(9,3)\|CO2 REMOVAL(8,4)\|OLIVINE POWDER(8,2)\|ANTHROPOGENIC OXIDATION(8,1)\|CARBONATION REACTOR(8,1)\|INTENSE PREPROCESSING(8,1)\|MAGNESIA DISSOLVE(8,1)\|MAGNESIA POWDER SUSPENSION(8,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(8,1)\|MINERAL CARBONATION REACTION(8,1)\|MINERAL SEQUESTRATION(8,1)\|NONINVENTIVE EXPERIMENT(8,1)\|OLIVINE DIGESTION(8,1)\|SCALABILITY EXPERIMENT(8,1)\|DATA POINT(7,2)\|INORGANIC POWDER(7,2)\|MAGNESIUM SILICATE CONVERSION(7,2)\|MG3SI2O(7,2)\|STEP CONDITION(7,2)\|BRUCITE SOLUBILITY(7,1)\|CARBONACEOUS FOSSIL FUEL(7,1)\|CO2 DISSOLUTION(7,1)\|CO2 TONNE(7,1)\|ELEMENTAL CONSTITUENT(7,1)\|HUGE ENERGY PENALTY(7,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(7,1)\|MASTER THESIS(7,1)\|MINERAL DIGESTION(7,1)\|MINERALOGICAL SITE(7,1)\|MINING HIGH COST(7,1)\|OLIVINE CONVERSION(7,1)\|OVERNIGHT SHUTDOWN(7,1)\|UTILIZATION OPTION(7,1)\|VESSEL PRESSURIZATION(7,1)\|WOLLASTONITE(6,3)\|ROTAMETER(6,2)\|ALKALINE REAGENT(6,1)\|AQUEOUS MAGNESIA(6,1)\|BRUCITE CONVERSION(6,1)\|BRUCITE MINOR PHASE(6,1)\|BRUCITE POWDER(6,1)\|CO2 METER(6,1)\|CO2 TRANSPORT(6,1)\|CYLINDER PREMIX(6,1)\|DIGESTION VESSEL(6,1)\|DUNITE POWDER(6,1)\|INLET CO2(6,1)\|MAGNESIA YIELD(6,1)\|MAGNESIUM ION(6,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(6,1)\|MAGNESIUM SILICATE MINERAL POWDER(6,1)\|METAL SILICATE CARBONATION(6,1)\|MINERAL HYDROXIDE(6,1)\|MOLE RATION(6,1)\|OCCASIONAL MEASUREMENT(6,1)\|PARTICLE ATTRITION(6,1)\|PREMIX CYLINDER(6,1)\|PRESSURIZATION DEPRESSURIZATION(6,1)\|SAMPLE XRD PATTERN(6,1)\|SLURRY CIRCULATION(6,1)\|SLURRY DROPLET SOLUTION(6,1)\|STABLE MINERAL CARBONATE(6,1)\|STOICHIOMETRIC CONVERSION(6,1)\|VALUABLE MINERAL(6,1)\|AMBIENT ATMOSPHERIC PRESSURE(5,4)\|ALKALINE EARTH SILICATE(5,3)\|CAUSTIC ALKALI METAL HYDROXIDE(5,2)\|HIGH COST(5,2)\|MG2SIO(5,2)\|PRODUCTION THROUGHPUT(5,2)\|SEAWATER(5,2)\|ABUNDANT SOURCE(5,1)\|ACIDIC PRETREATMENT(5,1)\|AGEING(5,1)\|ALKALI TREATMENT(5,1)\|ALKALINE PH(5,1)\|AMBIENT ATMOSPHERE(5,1)\|BLEND CONTENT(5,1)\|BRUCITE MAJOR PHASE(5,1)\|BUBBLE COLUMN(5,1)\|CALCIUM SILICATE MINERAL(5,1)\|CALIBRATED GLASS TUBE ROTAMMETER(5,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(5,1)\|CO2 EMISSION DISTANT SOURCE(5,1)\|CO2 SEQUESTRATION CAPACITY(5,1)\|CONTRADISTINCTION(5,1)\|DOMINANT REACTION(5,1)\|DRY STOICHIOMETRIC REACTION(5,1)\|EARTH ATMOSPHERE(5,1)\|ELECTRICITY GENERATING FACILITY(5,1)\|FEED MINERAL(5,1)\|GEOLOGIC TIMESCALE(5,1)\|GLASS SOLIDIFICATION(5,1)\|HUGE SCALE(5,1)\|HYDROTHERMAL REACTION SAVE(5,1)\|INFRARED DATA LOGGER(5,1)\|INLET GAS CO2(5,1)\|INORGANIC PARTICLE(5,1)\|MAGNESIA PRODUCTION(5,1)\|MAGNESIUM BICARBONATE MG(5,1)\|MAGNESIUM SILICATE CRYSTAL(5,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(5,1)\|MAGNESIUM SILICATE PARTICLE(5,1)\|MAGNESIUM SILICATE POWDER(5,1)\|METHANEDIONE SOURCE(5,1)\|MONITORED EXIT GAS(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONEXCLUSIVE(5,1)\|OLIVINE REACTION(5,1)\|PRECAPTURE(5,1)\|PRIMARY INITIATIVE(5,1)\|QUANTITATIVE PHASE ANALYSIS(5,1)\|REACTION ACCELERATOR(5,1)\|RELIANCE(5,1)\|SALABLE CHEMICAL(5,1)\|SEALED VESSEL(5,1)\|SODIUM HYDROXIDE REGENERATION(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|UNPRESSURIZED CONTINUOUS MODE(5,1)\|UNPRESSURIZED REACTION VESSEL(5,1)\|REACTION PRODUCT(4,6)\|HCO(4,3)\|NONUNDERLINED NUMBER(4,3)\|TEMPERATURE ELEVATION(4,3)\|UNDERLINED NUMERAL(4,3)\|2H2O(4,2)\|STOICHIOMETRIC RATIO(3,4)\|ABSOLUTE UNCERTAINTY(3,1)\|ALKALI DIGESTION(3,1)\|ALKALINE COMPOUND INPUT(3,1)\|ALKALINE SOLUTION(3,1)\|ANTIGORITE(3,1)\|AQUEOUS PHASE CARBONATION(3,1)\|AQUEOUS REACTION(3,1)\|AUTOCLAVE(3,1)\|BOUND HYDROXIDE GROUP(3,1)\|CARBONATION DETAIL(3,1)\|CHRYSOTILE(3,1)\|CLEAR BENEFIT(3,1)\|CO2 CONCENTRATION CHANGE(3,1)\|CO2 DEPLETED GAS(3,1)\|CO2 MASS(3,1)\|COMPACTION(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CONCERN CAUSE(3,1)\|CONTAMINATION(3,1)\|DISCOVERY(3,1)\|DISSOLUTION DISINTEGRATION(3,1)\|ECONOMIC FEASIBILITY(3,1)\|EXCESS ALKALI(3,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(3,1)\|\|(US9963351)\|MAGNESIA(100,40)\|MAGNESIUM SILICATE(100,33)\|MAGNESIUM SILICATE MINERAL(100,14)\|ACTIVATION(100,6)\|MINERAL SILICATE MINERAL ACTIVATION(100,1)\|MINERAL CARBONATION(79,6)\|INEFFICIENCY(60,2)\|OLIVINE CONVERSION(60,1)\|UNPRESSURIZED VESSEL(59,6)\|METHANEDIONE SEQUESTRATION(52,6)\|ALKALINE AQUEOUS LIQUID SLURRY(50,4)\|ALKALI DIGESTION(48,1)\|SHELL INTERNATIONAL(45,1)\|SERPENTINE MINERAL(43,1)\|DRY POWDER(41,4)\|OLIVINE ROCK(41,1)\|ENERGY WASTAGE(38,1)\|SODIUM HYDROXIDE REGENERATION(38,1)\|MAGNESIUM SILICATE DRY POWDER(37,2)\|CONTRADISTINCTION(35,1)\|EXPERIMENTAL CONDITION EXPLORATION(35,1)\|INDIRECT SEQUESTRATION(35,1)\|NATURALLY OCCURRING OLIVINE(35,1)\|EQUIPMENT COMPLICATION(33,1)\|EXPENSIVE EQUIPMENT(33,1)\|METHANEDIONE(32,42)\|OLIVINE SODIUM HYDROXIDE REACTION(32,1)\|MAGNESIUM SILICATE ROCK(31,1)\|ROCK(31,1)\|ALKALI METAL SILICATE(29,5)\|AQUEOUS SOLUTION(28,16)\|CARBONATION DETAIL(28,1)\|MOLAR RATIO(27,6)\|ALKALI DIGESTION(27,1)\|BRUCITE(22,22)\|SEQUESTRATION(22,10)\|SEQUESTRATING METHANEDIONE(22,4)\|OPEN VESSEL(21,1)\|AQUEOUS PHASE PRODUCTION(19,4)\|SODIUM CARBONATE(17,4)\|REACTION PRESSURE(17,1)\|SODIUM HYDROXIDE(16,72)\|SOLID GLASS PRODUCT(16,5)\|EXPERIMENTAL CONDITION(16,1)\|GLASS PRODUCT(15,5)\|TEMPERATURE ELEVATION(15,4)\|SUSPENDED BRUCITE PARTICLE(15,3)\|FORSTERITE CAREFUL QUANTIFICATION(15,1)\|SERPENTINE FEEDSTOCK TONNE(15,1)\|ALKALI METAL HYDROXIDE(14,6)\|ALKALI METAL(13,20)\|ATMOSPHERIC PRESSURE(13,10)\|TEMPORAL DURATION(13,4)\|MINERAL FEEDSTOCK CARBONATION(13,1)\|FLUE GAS(12,24)\|SOLID PRODUCT(12,10)\|ALKALINE EARTH SILICATE(12,8)\|AMBIENT ATMOSPHERIC PRESSURE(12,7)\|SALABLE INDUSTRIAL FEEDSTOCK(12,1)\|CO2 SCRUBBING(11,2)\|BRUCITE CARBONATION(11,1)\|CONTEMPORARY RESEARCH OVERVIEW(11,1)\|MAGNESIA CARBONATION(11,1)\|MAGNESIA TONNE(11,1)\|METHANEDIONE TONNE(11,1)\|MINERAL CARBONATION SCIENCE(11,1)\|OLIVINE CARBONATION(11,1)\|SEQUESTRATION METHANEDIONE(11,1)\|UNPRESSURIZED AQUEOUS CARBONATION(11,1)\|DGC REACTOR(10,2)\|BLENCOE ASSERTION(10,1)\|BRUCITE QUANTIFICATION(10,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(10,1)\|RIETVELD REFINEMENT QPA(10,1)\|SATISFACTORY MINERAL CARBONATION(10,1)\|SERPENTINE DEHYDROXYLATION(10,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(10,1)\|BICARBONATE ION(9,3)\|WATER VAPOR PRESSURE(9,3)\|CO2 REMOVAL(8,4)\|MAGNESIUM SILICATE CONVERSION(8,3)\|OLIVINE POWDER(8,2)\|ANTHROPOGENIC OXIDATION(8,1)\|CARBONATION REACTOR(8,1)\|INTENSE PREPROCESSING(8,1)\|MAGNESIA DISSOLVE(8,1)\|MAGNESIA POWDER SUSPENSION(8,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(8,1)\|MINERAL CARBONATION REACTION(8,1)\|MINERAL SEQUESTRATION(8,1)\|OLIVINE DIGESTION(8,1)\|PROPOSED MINERAL CARBONATION(8,1)\|SCALABILITY EXPERIMENT(8,1)\|VAPOR PRESSURE(7,8)\|WOLLASTONITE(7,4)\|BLEND CONTENT(7,2)\|ENERGY EFFICIENCY(7,2)\|EXPERIMENTAL PATTERN(7,2)\|INORGANIC POWDER(7,2)\|METHANEDIONE SOURCE(7,2)\|UNPRESSURIZED CONTINUOUS MODE(7,2)\|BRUCITE DISPERSION(7,1)\|BRUCITE POWDER SEPARATION(7,1)\|BRUCITE PROPORTION(7,1)\|BRUCITE SOLUBILITY(7,1)\|CARBONACEOUS FOSSIL FUEL(7,1)\|CO2 DISSOLUTION(7,1)\|CO2 TONNE(7,1)\|DIRT ATTRITION(7,1)\|ELEMENTAL CONSTITUENT(7,1)\|HUGE ENERGY PENALTY(7,1)\|MAGNESIA INTEREST(7,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(7,1)\|MASTER THESIS(7,1)\|MINERAL DIGESTION(7,1)\|MINERALOGICAL SITE(7,1)\|MINING HIGH COST(7,1)\|OVERNIGHT SHUTDOWN(7,1)\|SILICATE MINERAL CARBONATION(7,1)\|STIRRED TEFLON VESSEL(7,1)\|UTILIZATION OPTION(7,1)\|VESSEL PRESSURIZATION(7,1)\|MG2SIO(6,3)\|EXCESS CONSUMPTION(6,2)\|ROTAMETER(6,2)\|ALKALINE REAGENT(6,1)\|AMBIENT UNPRESSURIZED CONDITION(6,1)\|AQUEOUS MAGNESIA(6,1)\|BRUCITE CONVERSION(6,1)\|BRUCITE MINOR PHASE(6,1)\|CO2 ED(6,1)\|CO2 TRANSPORT(6,1)\|CYLINDER PREMIX(6,1)\|DIGESTION VESSEL(6,1)\|DUNITE POWDER(6,1)\|H2O MOLAR RATIO(6,1)\|INLET CO2(6,1)\|MAGNESIA YIELD(6,1)\|MAGNESIUM ION(6,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(6,1)\|MAGNESIUM SILICATE MINERAL POWDER(6,1)\|METAL SILICATE CARBONATION(6,1)\|MINERAL HYDROXIDE(6,1)\|MOLE RATION(6,1)\|OCCASIONAL MEASUREMENT(6,1)\|PARTICLE ATTRITION(6,1)\|PREMIX CYLINDER(6,1)\|SAMPLE XRD PATTERN(6,1)\|SLURRY CIRCULATION(6,1)\|SLURRY DROPLET SOLUTION(6,1)\|STABLE MINERAL CARBONATE(6,1)\|STOICHIOMETRIC CONVERSION(6,1)\|STOICHIOMETRIC MOLAR RATIO(6,1)\|VALUABLE MINERAL(6,1)\|WATER CARBONATION REACTION(6,1)\|HCO(5,5)\|MGCO(5,4)\|CAUSTIC ALKALI METAL HYDROXIDE(5,2)\|METAL MINERAL SILICATE DIGESTION(5,2)\|MODEL CALCULATION(5,2)\|MOLALITY(5,2)\|PRODUCTION THROUGHPUT(5,2)\|SEAWATER(5,2)\|ABUNDANT SOURCE(5,1)\|ACIDIC PRETREATMENT(5,1)\|AGEING(5,1)\|ALKALI TREATMENT(5,1)\|ALKALINE PH(5,1)\|AMBIENT ATMOSPHERE(5,1)\|BRUCITE MAJOR PHASE(5,1)\|BUBBLE COLUMN(5,1)\|CALCIUM SILICATE MINERAL(5,1)\|CALIBRATED GLASS TUBE ROTAMMETER(5,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(5,1)\|CO2 EMISSION DISTANT SOURCE(5,1)\|CO2 EXPENSIVE SEPARATION(5,1)\|CO2 REACTION(5,1)\|CO2 SEQUESTRATION CAPACITY(5,1)\|DOMINANT REACTION(5,1)\|DRY STOICHIOMETRIC REACTION(5,1)\|EARTH ATMOSPHERE(5,1)\|ELECTRICITY GENERATING FACILITY(5,1)\|FEED MINERAL(5,1)\|GEOLOGIC TIMESCALE(5,1)\|GLASS SOLIDIFICATION(5,1)\|HUGE SCALE(5,1)\|HYDROTHERMAL REACTION SAVE(5,1)\|INFRARED DATA LOGGER(5,1)\|INLET GAS CO2(5,1)\|INORGANIC PARTICLE(5,1)\|MAGNESIA PRODUCTION(5,1)\|MAGNESIA WEIGHT(5,1)\|MAGNESIUM BICARBONATE MG(5,1)\|MAGNESIUM SILICATE CRYSTAL(5,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(5,1)\|MAGNESIUM SILICATE PARTICLE(5,1)\|MAGNESIUM SILICATE POWDER(5,1)\|MONITORED EXIT GAS(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONEXCLUSIVE(5,1)\|OLIVINE REACTION(5,1)\|PRECAPTURE(5,1)\|PRESSURIZATION DEPRESSURIZATION(5,1)\|PRIMARY INITIATIVE(5,1)\|QUANTITATIVE PHASE ANALYSIS(5,1)\|REACTION ACCELERATOR(5,1)\|REACTION SOLUBLE FRACTION(5,1)\|RELIANCE(5,1)\|SALABLE CHEMICAL(5,1)\|SEALED VESSEL(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|UNPRESSURIZED REACTION VESSEL(5,1)\|UNSEPARATED FLUE GAS(5,1)\|REACTION PRODUCT(4,7)\|NONUNDERLINED NUMBER(4,3)\|UNDERLINED NUMERAL(4,3)\|GAS MIXTURE(3,10)\|STOICHIOMETRIC RATIO(3,4)\|ABSOLUTE UNCERTAINTY(3,1)\|ALKALINE COMPOUND INPUT(3,1)\|ALKALINE SOLUTION(3,1)\|AMBIENT PRESSURE CARBONATION(3,1)\|ANTIGORITE(3,1)\|AQUEOUS PHASE CARBONATION(3,1)\|AQUEOUS REACTION(3,1)\|AUTOCLAVE(3,1)\|BLENDING SYSTEM(3,1)\|BOUND HYDROXIDE GROUP(3,1)\|CHRYSOTILE(3,1)\|CLEAR BENEFIT(3,1)\|CO2 CONCENTRATION CHANGE(3,1)\|CO2 DEPLETED GAS(3,1)\|CO2 MASS(3,1)\|COMPACTION(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CONCERN CAUSE(3,1)\|CONSUMPTION CONDITION(3,1)\|CONTAMINATION(3,1)\|DIFFERENCE PLOT(3,1)\|DISCOVERY(3,1)\|DISSOLUTION DISINTEGRATION(3,1)\|ECONOMIC FEASIBILITY(3,1)\|EXCESS ALKALI(3,1)\|\|(US20170029284)\|MAGNESIA(100,40)\|MAGNESIUM SILICATE(100,33)\|MAGNESIUM SILICATE MINERAL(100,14)\|ACTIVATION(100,6)\|MINERAL SILICATE MINERAL ACTIVATION(100,1)\|MINERAL CARBONATION(79,6)\|INEFFICIENCY(60,2)\|OLIVINE CONVERSION(60,1)\|UNPRESSURIZED VESSEL(59,6)\|METHANEDIONE SEQUESTRATION(52,6)\|ALKALI DIGESTION(48,1)\|SHELL INTERNATIONAL(45,1)\|ALKALINE AQUEOUS LIQUID SLURRY(43,3)\|SERPENTINE MINERAL(43,1)\|DRY POWDER(41,4)\|OLIVINE ROCK(41,1)\|ENERGY WASTAGE(38,1)\|SODIUM HYDROXIDE REGENERATION(38,1)\|MAGNESIUM SILICATE DRY POWDER(37,2)\|CONTRADISTINCTION(35,1)\|EXPERIMENTAL CONDITION EXPLORATION(35,1)\|INDIRECT SEQUESTRATION(35,1)\|NATURALLY OCCURRING OLIVINE(35,1)\|EQUIPMENT COMPLICATION(33,1)\|EXPENSIVE EQUIPMENT(33,1)\|METHANEDIONE(32,42)\|OLIVINE SODIUM HYDROXIDE REACTION(32,1)\|MAGNESIUM SILICATE ROCK(31,1)\|ROCK(31,1)\|ALKALI METAL SILICATE(29,5)\|AQUEOUS SOLUTION(28,16)\|CARBONATION DETAIL(28,1)\|MOLAR RATIO(27,6)\|ALKALI DIGESTION(27,1)\|BRUCITE(22,22)\|SEQUESTRATION(22,10)\|SEQUESTRATING METHANEDIONE(22,4)\|OPEN VESSEL(21,1)\|AQUEOUS PHASE PRODUCTION(19,4)\|CO2 SEQUESTRATION(19,2)\|SODIUM CARBONATE(17,4)\|REACTION PRESSURE(17,1)\|SODIUM HYDROXIDE(16,72)\|SOLID GLASS PRODUCT(16,5)\|EXPERIMENTAL CONDITION(16,1)\|GLASS PRODUCT(15,5)\|TEMPERATURE ELEVATION(15,4)\|SUSPENDED BRUCITE PARTICLE(15,3)\|FORSTERITE CAREFUL QUANTIFICATION(15,1)\|SERPENTINE FEEDSTOCK TONNE(15,1)\|ALKALI METAL HYDROXIDE(14,6)\|ALKALI METAL(13,20)\|ATMOSPHERIC PRESSURE(13,10)\|TEMPORAL DURATION(13,4)\|MINERAL FEEDSTOCK CARBONATION(13,1)\|FLUE GAS(12,24)\|SOLID PRODUCT(12,10)\|ALKALINE EARTH SILICATE(12,8)\|AMBIENT ATMOSPHERIC PRESSURE(12,7)\|SALABLE INDUSTRIAL FEEDSTOCK(12,1)\|CO2 SCRUBBING(11,2)\|BRUCITE CARBONATION(11,1)\|CONTEMPORARY RESEARCH OVERVIEW(11,1)\|MAGNESIA CARBONATION(11,1)\|MAGNESIA TONNE(11,1)\|METHANEDIONE TONNE(11,1)\|MINERAL CARBONATION SCIENCE(11,1)\|OLIVINE CARBONATION(11,1)\|SEQUESTRATION METHANEDIONE(11,1)\|UNPRESSURIZED AQUEOUS CARBONATION(11,1)\|DGC REACTOR(10,2)\|BLENCOE ASSERTION(10,1)\|BRUCITE QUANTIFICATION(10,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(10,1)\|RIETVELD REFINEMENT QPA(10,1)\|SATISFACTORY MINERAL CARBONATION(10,1)\|SERPENTINE DEHYDROXYLATION(10,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(10,1)\|BICARBONATE ION(9,3)\|WATER VAPOR PRESSURE(9,3)\|CO2 REMOVAL(8,4)\|MAGNESIUM SILICATE CONVERSION(8,3)\|OLIVINE POWDER(8,2)\|ANTHROPOGENIC OXIDATION(8,1)\|CARBONATION REACTOR(8,1)\|INTENSE PREPROCESSING(8,1)\|MAGNESIA DISSOLVE(8,1)\|MAGNESIA POWDER SUSPENSION(8,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(8,1)\|MINERAL CARBONATION REACTION(8,1)\|MINERAL SEQUESTRATION(8,1)\|OLIVINE DIGESTION(8,1)\|PROPOSED MINERAL CARBONATION(8,1)\|SCALABILITY EXPERIMENT(8,1)\|VAPOR PRESSURE(7,8)\|WOLLASTONITE(7,4)\|BLEND CONTENT(7,2)\|ENERGY EFFICIENCY(7,2)\|EXPERIMENTAL PATTERN(7,2)\|INORGANIC POWDER(7,2)\|METHANEDIONE SOURCE(7,2)\|UNPRESSURIZED CONTINUOUS MODE(7,2)\|BRUCITE DISPERSION(7,1)\|BRUCITE POWDER SEPARATION(7,1)\|BRUCITE PROPORTION(7,1)\|BRUCITE SOLUBILITY(7,1)\|CARBONACEOUS FOSSIL FUEL(7,1)\|CO2 DISSOLUTION(7,1)\|CO2 TONNE(7,1)\|ELEMENTAL CONSTITUENT(7,1)\|HUGE ENERGY PENALTY(7,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(7,1)\|MASTER THESIS(7,1)\|MINERAL DIGESTION(7,1)\|MINERALOGICAL SITE(7,1)\|MINING HIGH COST(7,1)\|OVERNIGHT SHUTDOWN(7,1)\|SILICATE MINERAL CARBONATION(7,1)\|STIRRED TEFLON VESSEL(7,1)\|UTILIZATION OPTION(7,1)\|VESSEL PRESSURIZATION(7,1)\|EXCESS CONSUMPTION(6,2)\|ROTAMETER(6,2)\|ALKALINE REAGENT(6,1)\|AMBIENT UNPRESSURIZED CONDITION(6,1)\|AQUEOUS MAGNESIA(6,1)\|BRUCITE CONVERSION(6,1)\|BRUCITE MINOR PHASE(6,1)\|CO2 METER(6,1)\|CO2 TRANSPORT(6,1)\|COSEQUESTRATION CAPACITY(6,1)\|CYLINDER PREMIX(6,1)\|DIGESTION VESSEL(6,1)\|DUNITE POWDER(6,1)\|H2O MOLAR RATIO(6,1)\|INLET CO2(6,1)\|MAGNESIA FORMATION(6,1)\|MAGNESIA YIELD(6,1)\|MAGNESIUM ION(6,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(6,1)\|MAGNESIUM SILICATE MINERAL POWDER(6,1)\|METAL SILICATE CARBONATION(6,1)\|MINERAL HYDROXIDE(6,1)\|MOLE RATION(6,1)\|OCCASIONAL MEASUREMENT(6,1)\|PARTICLE ATTRITION(6,1)\|PREMIX CYLINDER(6,1)\|SAMPLE XRD PATTERN(6,1)\|SLURRY CIRCULATION(6,1)\|SLURRY DROPLET SOLUTION(6,1)\|STABLE MINERAL CARBONATE(6,1)\|STOICHIOMETRIC CONVERSION(6,1)\|STOICHIOMETRIC MOLAR RATIO(6,1)\|VALUABLE MINERAL(6,1)\|WATER CARBONATION REACTION(6,1)\|HCO(5,4)\|CAUSTIC ALKALI METAL HYDROXIDE(5,2)\|LITER WATER(5,2)\|METAL MINERAL SILICATE DIGESTION(5,2)\|MG2SIO(5,2)\|MODEL CALCULATION(5,2)\|MOLALITY(5,2)\|PRODUCTION THROUGHPUT(5,2)\|SEAWATER(5,2)\|ABUNDANT SOURCE(5,1)\|ACIDIC PRETREATMENT(5,1)\|AGEING(5,1)\|ALKALI TREATMENT(5,1)\|ALKALINE PH(5,1)\|AMBIENT ATMOSPHERE(5,1)\|BRUCITE MAJOR PHASE(5,1)\|BUBBLE COLUMN(5,1)\|CALCIUM SILICATE MINERAL(5,1)\|CALIBRATED GLASS TUBE ROTAMMETER(5,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(5,1)\|CO2 EMISSION DISTANT SOURCE(5,1)\|CO2 EXPENSIVE SEPARATION(5,1)\|CO2 REACTION(5,1)\|DOMINANT REACTION(5,1)\|DRY STOICHIOMETRIC REACTION(5,1)\|EARTH ATMOSPHERE(5,1)\|ELECTRICITY GENERATING FACILITY(5,1)\|FEED MINERAL(5,1)\|GEOLOGIC TIMESCALE(5,1)\|GLASS SOLIDIFICATION(5,1)\|HUGE SCALE(5,1)\|HYDROTHERMAL REACTION SAVE(5,1)\|INFRARED DATA LOGGER(5,1)\|INLET GAS CO2(5,1)\|INORGANIC PARTICLE(5,1)\|MAGNESIA PRODUCTION(5,1)\|MAGNESIA WEIGHT(5,1)\|MAGNESIUM BICARBONATE MG(5,1)\|MAGNESIUM SILICATE CRYSTAL(5,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(5,1)\|MAGNESIUM SILICATE PARTICLE(5,1)\|MAGNESIUM SILICATE POWDER(5,1)\|MONITORED EXIT GAS(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONEXCLUSIVE(5,1)\|OLIVINE REACTION(5,1)\|PRECAPTURE(5,1)\|PRESSURIZATION DEPRESSURIZATION(5,1)\|PRIMARY INITIATIVE(5,1)\|QUANTITATIVE PHASE ANALYSIS(5,1)\|REACTION ACCELERATOR(5,1)\|REACTION SOLUBLE FRACTION(5,1)\|RELIANCE(5,1)\|SALABLE CHEMICAL(5,1)\|SEALED VESSEL(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|UNPRESSURIZED REACTION VESSEL(5,1)\|UNSEPARATED FLUE GAS(5,1)\|REACTION PRODUCT(4,7)\|MGCO(4,3)\|NONUNDERLINED NUMBER(4,3)\|UNDERLINED NUMERAL(4,3)\|GAS MIXTURE(3,10)\|STOICHIOMETRIC RATIO(3,4)\|ABSOLUTE UNCERTAINTY(3,1)\|ALKALINE COMPOUND INPUT(3,1)\|ALKALINE SOLUTION(3,1)\|AMBIENT PRESSURE CARBONATION(3,1)\|ANTIGORITE(3,1)\|AQUEOUS PHASE CARBONATION(3,1)\|AQUEOUS REACTION(3,1)\|AUTOCLAVE(3,1)\|BLENDING SYSTEM(3,1)\|BOUND HYDROXIDE GROUP(3,1)\|CHRYSOTILE(3,1)\|CLEAR BENEFIT(3,1)\|CO2 CONCENTRATION CHANGE(3,1)\|CO2 DEPLETED GAS(3,1)\|CO2 MASS(3,1)\|COMPACTION(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CONCERN CAUSE(3,1)\|CONSUMPTION CONDITION(3,1)\|CONTAMINATION(3,1)\|DIFFERENCE PLOT(3,1)\|\|(WO2015/154887)\|MAGNESIA(100,38)\|MAGNESIUM SILICATE(100,31)\|MAGNESIUM SILICATE MINERAL(100,14)\|UNPRESSURIZED VESSEL(100,6)\|ACTIVATION(100,5)\|DRY POWDER(69,4)\|MAGNESIUM SILICATE DRY POWDER(62,2)\|ALKALINE AQUEOUS LIQUID SLURRY(56,2)\|MOLAR RATIO(46,6)\|METHANEDIONE SEQUESTRATION(43,5)\|BLEND CONTENT(37,2)\|ALKALINE COMPOUND(35,9)\|DISSOLUTION(35,9)\|AQUEOUS SOLUTION(34,14)\|SEQUESTRATING METHANEDIONE(32,3)\|SODIUM CARBONATE(32,3)\|ALKALI METAL SILICATE(30,3)\|SOLID GLASS PRODUCT(25,4)\|SUSPENDED BRUCITE PARTICLE(25,3)\|FORSTERITE CAREFUL QUANTIFICATION(25,1)\|SERPENTINE FEEDSTOCK TONNE(25,1)\|GLASS PRODUCT(23,4)\|TEMPORAL DURATION(23,4)\|REACTION CHAMBER BLENDING CONTENT(23,2)\|MINERAL FEEDSTOCK CARBONATION(23,1)\|SALABLE INDUSTRIAL FEEDSTOCK(21,1)\|AQUEOUS PHASE PRODUCTION(20,2)\|CO2 SCRUBBING(19,2)\|BRUCITE CARBONATION(19,1)\|CONTEMPORARY RESEARCH OVERVIEW(19,1)\|MAGNESIA CARBONATION(19,1)\|MAGNESIA TONNE(19,1)\|METHANEDIONE TONNE(19,1)\|MINERAL CARBONATION SCIENCE(19,1)\|OLIVINE CARBONATION(19,1)\|SEQUESTRATION METHANEDIONE(19,1)\|UNPRESSURIZED AQUEOUS CARBONATION(19,1)\|DGC REACTOR(17,2)\|BLENCOE ASSERTION(16,1)\|BRUCITE QUANTIFICATION(16,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(16,1)\|RIETVELD REFINEMENT QPA(16,1)\|SATISFACTORY MINERAL CARBONATION(16,1)\|SERPENTINE DEHYDROXYLATION(16,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(16,1)\|ALKALI METAL(15,15)\|BICARBONATE ION(15,3)\|MAGNESIUM SILICATE CONVERSION(14,3)\|OLIVINE POWDER(14,2)\|ANTHROPOGENIC OXIDATION(14,1)\|CARBONATION REACTOR(14,1)\|INTENSE PREPROCESSING(14,1)\|MAGNESIA DISSOLVE(14,1)\|MAGNESIA POWDER SUSPENSION(14,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(14,1)\|MINERAL CARBONATION REACTION(14,1)\|MINERAL SEQUESTRATION(14,1)\|OLIVINE DIGESTION(14,1)\|PROPOSED MINERAL CARBONATION(14,1)\|SCALABILITY EXPERIMENT(14,1)\|CO2 REMOVAL(13,4)\|STEP CONDITION(13,2)\|WOLLASTONITE(12,4)\|BRUCITE DISPERSION(12,1)\|BRUCITE POWDER SEPARATION(12,1)\|BRUCITE SOLUBILITY(12,1)\|CARBONACEOUS FOSSIL FUEL(12,1)\|CO2 TONNE(12,1)\|ELEMENTAL CONSTITUENT(12,1)\|HUGE ENERGY PENALTY(12,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(12,1)\|MASTER THESIS(12,1)\|MINERAL DIGESTION(12,1)\|MINERALOGICAL SITE(12,1)\|OVERNIGHT SHUTDOWN(12,1)\|SILICATE MINERAL CARBONATION(12,1)\|STIRRED TEFLON VESSEL(12,1)\|UTILIZATION OPTION(12,1)\|VESSEL PRESSURIZATION(12,1)\|ALKALI METAL COMPOUND(11,9)\|ALKALINE EARTH SILICATE(11,5)\|EXPERIMENTAL PATTERN(11,2)\|INORGANIC POWDER(11,2)\|METHANEDIONE SOURCE(11,2)\|UNPRESSURIZED CONTINUOUS MODE(11,2)\|AMBIENT ATMOSPHERIC PRESSURE(10,6)\|EXCESS CONSUMPTION(10,2)\|ROTAMETER(10,2)\|ALKALINE REAGENT(10,1)\|AMBIENT UNPRESSURIZED CONDITION(10,1)\|AQUEOUS MAGNESIA(10,1)\|BRUCITE CONVERSION(10,1)\|BRUCITE MINOR PHASE(10,1)\|CO2 METER(10,1)\|CO2 TRANSPORT(10,1)\|CYLINDER PREMIX(10,1)\|DIGESTION VESSEL(10,1)\|DUNITE POWDER(10,1)\|INLET CO2(10,1)\|MAGNESIA FORMATION(10,1)\|MAGNESIA YIELD(10,1)\|MAGNESIUM ION(10,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(10,1)\|MAGNESIUM SILICATE MINERAL POWDER(10,1)\|METAL SILICATE CARBONATION(10,1)\|MINERAL HYDROXIDE(10,1)\|MOLE RATION(10,1)\|OCCASIONAL MEASUREMENT(10,1)\|PARTICLE ATTRITION(10,1)\|PREMIX CYLINDER(10,1)\|PRESSURIZATION DEPRESSURIZATION(10,1)\|SAMPLE XRD PATTERN(10,1)\|SLURRY CIRCULATION(10,1)\|SLURRY DROPLET SOLUTION(10,1)\|STABLE MINERAL CARBONATE(10,1)\|STOICHIOMETRIC CONVERSION(10,1)\|STOICHIOMETRIC MOLAR RATIO(10,1)\|VALUABLE MINERAL(10,1)\|WATER CARBONATION REACTION(10,1)\|DIGESTION(9,5)\|TEMPERATURE ELEVATION(8,4)\|BICARBONATE SOLUTION(8,2)\|CAUSTIC ALKALI METAL HYDROXIDE(8,2)\|LITER WATER(8,2)\|MODEL CALCULATION(8,2)\|MOLALITY(8,2)\|PRODUCTION THROUGHPUT(8,2)\|SEAWATER(8,2)\|ABUNDANT SOURCE(8,1)\|ACIDIC PRETREATMENT(8,1)\|AGEING(8,1)\|ALKALI TREATMENT(8,1)\|ALKALINE PH(8,1)\|AMBIENT ATMOSPHERE(8,1)\|BRUCITE MAJOR PHASE(8,1)\|BUBBLE COLUMN(8,1)\|CALCIUM SILICATE MINERAL(8,1)\|CALIBRATED GLASS TUBE ROTAMMETER(8,1)\|CIRCULATING LIQUID PERIODIC SAMPLE(8,1)\|CO2 EMISSION DISTANT SOURCE(8,1)\|CO2 EXPENSIVE SEPARATION(8,1)\|CO2 REACTION(8,1)\|CO2 SEQUESTRATION CAPACITY(8,1)\|DOMINANT REACTION(8,1)\|DRY STOICHIOMETRIC REACTION(8,1)\|EARTH ATMOSPHERE(8,1)\|ELECTRICITY GENERATING FACILITY(8,1)\|FEED MINERAL(8,1)\|GEOLOGIC TIMESCALE(8,1)\|GLASS SOLIDIFICATION(8,1)\|HUGE SCALE(8,1)\|HYDROTHERMAL REACTION SAVE(8,1)\|INFRARED DATA LOGGER(8,1)\|INLET GAS CO2(8,1)\|INORGANIC PARTICLE(8,1)\|INTIAL(8,1)\|MAGNESIA PRODUCTION(8,1)\|MAGNESIA WEIGHT(8,1)\|MAGNESIUM BICARBONATE MG(8,1)\|MAGNESIUM SILICATE CRYSTAL(8,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(8,1)\|MAGNESIUM SILICATE PARTICLE(8,1)\|MAGNESIUM SILICATE POWDER(8,1)\|MINERAL SILICATE ACTIVATION(8,1)\|MONITORED EXIT GAS(8,1)\|NATURALLY OCCURRING FEEDSTOCK(8,1)\|NONEXCLUSIVE(8,1)\|OLIVINE REACTION(8,1)\|PRECAPTURE(8,1)\|PRIMARY INITIATIVE(8,1)\|QUANTITATIVE PHASE ANALYSIS(8,1)\|REACTION ACCELERATOR(8,1)\|REACTION SOLUBLE FRACTION(8,1)\|RELIANCE(8,1)\|SALABLE CHEMICAL(8,1)\|SEALED VESSEL(8,1)\|STIRRED BED(8,1)\|STIRRED REACTOR(8,1)\|UNPRESSURIZED REACTION VESSEL(8,1)\|UNSEPARATED FLUE GAS(8,1)\|REACTION PRODUCT(7,7)\|S1O(7,3)\|UNDERLINED NUMERAL(7,3)\|GAS MIXTURE(6,10)\|STOICHIOMETRIC RATIO(6,4)\|ABSOLUTE UNCERTAINTY(6,1)\|ALKALINE COMPOUND INPUT(6,1)\|ALKALINE SOLUTION(6,1)\|AMBIENT PRESSURE CARBONATION(6,1)\|ANTIGORITE(6,1)\|AQUEOUS PHASE CARBONATION(6,1)\|AQUEOUS REACTION(6,1)\|AUTOCLAVE(6,1)\|BOUND HYDROXIDE GROUP(6,1)\|BYPRODUCT(6,1)\|CHRYSOTILE(6,1)\|CLEAR BENEFIT(6,1)\|CO2 MASS(6,1)\|COMPACTION(6,1)\|CONCENTRATED SODIUM HYDROXIDE(6,1)\|CONCERN CAUSE(6,1)\|CONSUMPTION CONDITION(6,1)\|CONTAMINATION(6,1)\|DIFFERENCE PLOT(6,1)\|DISCOVERY(6,1)\|DISSOLUTION DISINTEGRATION(6,1)\|ECONOMIC FEASIBILITY(6,1)\|EXCESS ALKALI(6,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(6,1)\|EXPERIMENTAL PERIOD(6,1)\|FIXED BED(6,1)\|GOVERNMENT(6,1)\|\|(GB2516141)\|MAGNESIA(100,31)\|MAGNESIUM SILICATE(100,27)\|MAGNESIUM SILICATE MINERAL(100,10)\|UNPRESSURIZED VESSEL(100,5)\|ACTIVATION(100,2)\|INEFFICIENCY(97,2)\|SHELL INTERNATIONAL(73,1)\|MINERAL CARBONATION(69,4)\|DRY POWDER(67,4)\|ENERGY WASTAGE(63,1)\|MAGNESIUM SILICATE DRY POWDER(60,2)\|INDIRECT SEQUESTRATION(56,1)\|METAL MINERAL SILICATE DIGESTION(56,1)\|ALKALINE AQUEOUS LIQUID SLURRY(54,2)\|METHANEDIONE(53,37)\|ROCK(50,1)\|MOLAR RATIO(48,4)\|METHANEDIONE SEQUESTRATION(37,4)\|METALLIC MINERAL SILICATE(36,1)\|DISSOLUTION(34,8)\|AQUEOUS SOLUTION(33,13)\|INDUSTRIAL PLANT(32,1)\|MINERAL SILICATE(31,2)\|SODIUM CARBONATE(28,4)\|ALKALI METAL SILICATE(27,4)\|SOLID GLASS PRODUCT(24,4)\|FORSTERITE CAREFUL QUANTIFICATION(24,1)\|SERPENTINE FEEDSTOCK TONNE(24,1)\|FLUE GAS(22,23)\|GLASS PRODUCT(22,4)\|TEMPORAL DURATION(22,4)\|MINERAL FEEDSTOCK CARBONATION(22,1)\|ALKALI METAL HYDROXIDE(21,7)\|AQUEOUS PHASE PRODUCTION(20,2)\|ENERGY EFFICIENCY(20,1)\|SALABLE INDUSTRIAL FEEDSTOCK(20,1)\|ALKALI METAL(19,23)\|ALKALINE COMPOUND(18,6)\|BRUCITE CARBONATION(18,1)\|CONTEMPORARY RESEARCH OVERVIEW(18,1)\|MAGNESIA CARBONATION(18,1)\|MAGNESIA TONNE(18,1)\|METHANEDIONE TONNE(18,1)\|MINERAL CARBONATION SCIENCE(18,1)\|OLIVINE CARBONATION(18,1)\|SEQUESTRATING METHANEDIONE(18,1)\|SEQUESTRATION METHANEDIONE(18,1)\|UNPRESSURIZED AQUEOUS CARBONATION(18,1)\|BLENCOE ASSERTION(16,1)\|BRUCITE QUANTIFICATION(16,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(16,1)\|RIETVELD REFINEMENT QPA(16,1)\|SATISFACTORY MINERAL CARBONATION(16,1)\|SERPENTINE DEHYDROXYLATION(16,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(16,1)\|STEP CONDITION(16,1)\|MAGNESIUM SILICATE CONVERSION(14,3)\|OLIVINE POWDER(14,2)\|ANTHROPOGENIC OXIDATION(14,1)\|CARBONATION REACTOR(14,1)\|CO2 SCRUBBING(14,1)\|INTENSE PREPROCESSING(14,1)\|MAGNESIA DISSOLVE(14,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(14,1)\|MINERAL CARBONATION REACTION(14,1)\|MINERAL SEQUESTRATION(14,1)\|OLIVINE DIGESTION(14,1)\|PROPOSED MINERAL CARBONATION(14,1)\|SCALABILITY EXPERIMENT(14,1)\|CAUSTIC ALKALI METAL HYDROXIDE(12,4)\|WOLLASTONITE(12,4)\|BRUCITE DISPERSION(12,1)\|BRUCITE POWDER SEPARATION(12,1)\|CARBONACEOUS FOSSIL FUEL(12,1)\|CO2 TONNE(12,1)\|HUGE ENERGY PENALTY(12,1)\|MAGNESIA POWDER(12,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(12,1)\|MASTER THESIS(12,1)\|METASTABLE CARBONATE(12,1)\|MINERALOGICAL SITE(12,1)\|MINING HIGH COST(12,1)\|SILICATE MINERAL CARBONATION(12,1)\|STIRRED TEFLON VESSEL(12,1)\|UTILIZATION OPTION(12,1)\|VESSEL PRESSURIZATION(12,1)\|EXPERIMENTAL PATTERN(11,2)\|INORGANIC POWDER(11,2)\|METHANEDIONE SOURCE(11,2)\|UNPRESSURIZED CONTINUOUS MODE(11,2)\|ALKALINE EARTH SILICATE(10,7)\|AMBIENT UNPRESSURIZED CONDITION(10,1)\|AQUEOUS MAGNESIA(10,1)\|BICARBONATE ION(10,1)\|CO2 TRANSPORT(10,1)\|DIGESTION VESSEL(10,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(10,1)\|MAGNESIUM SILICATE MINERAL POWDER(10,1)\|METAL SILICATE CARBONATION(10,1)\|MINERAL HYDROXIDE(10,1)\|PARTICLE ATTRITION(10,1)\|PRESSURIZATION DEPRESSURIZATION(10,1)\|SAMPLE XRD PATTERN(10,1)\|SLURRY CIRCULATION(10,1)\|SLURRY DROPLET SOLUTION(10,1)\|STABLE MINERAL CARBONATE(10,1)\|STOICHIOMETRIC CONVERSION(10,1)\|STOICHIOMETRIC MOLAR RATIO(10,1)\|WATER CARBONATION REACTION(10,1)\|AMBIENT ATMOSPHERIC PRESSURE(9,6)\|DIGESTION(9,5)\|ALKALI METAL BICARBONATE(8,4)\|ALKALI METAL CARBONATE(8,4)\|TEMPERATURE ELEVATION(8,4)\|HIGH COST(8,2)\|LITER WATER(8,2)\|MODEL CALCULATION(8,2)\|MOLALITY(8,2)\|PRODUCTION THROUGHPUT(8,2)\|SEAWATER(8,2)\|ABUNDANT SOURCE(8,1)\|ACIDIC PRETREATMENT(8,1)\|AGEING(8,1)\|ALKALI TREATMENT(8,1)\|ALKALINE PH(8,1)\|BRUCITE MAJOR PHASE(8,1)\|CALCIUM SILICATE MINERAL(8,1)\|CO2 EMISSION DISTANT SOURCE(8,1)\|CO2 EXPENSIVE SEPARATION(8,1)\|CO2 REACTION(8,1)\|CO2 SEQUESTRATION CAPACITY(8,1)\|DRY STOICHIOMETRIC REACTION(8,1)\|EARTH ATMOSPHERE(8,1)\|ELECTRICITY GENERATING FACILITY(8,1)\|FEED MINERAL(8,1)\|GEOLOGIC TIMESCALE(8,1)\|GLASS SOLIDIFICATION(8,1)\|HUGE SCALE(8,1)\|HYDROTHERMAL REACTION SAVE(8,1)\|INORGANIC PARTICLE(8,1)\|INTIAL(8,1)\|MAGNESIUM BICARBONATE MG(8,1)\|MAGNESIUM SILICATE CRYSTAL(8,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(8,1)\|MAGNESIUM SILICATE PARTICLE(8,1)\|MAGNESIUM SILICATE POWDER(8,1)\|MONITORED EXIT GAS(8,1)\|NATURALLY OCCURRING FEEDSTOCK(8,1)\|OLIVINE REACTION(8,1)\|PRIMARY INITIATIVE(8,1)\|QUANTITATIVE PHASE ANALYSIS(8,1)\|REACTION ACCELERATOR(8,1)\|REACTION SOLUBLE FRACTION(8,1)\|RELIANCE(8,1)\|SALABLE CHEMICAL(8,1)\|STIRRED BED(8,1)\|STIRRED REACTOR(8,1)\|UNPRESSURIZED REACTION VESSEL(8,1)\|UNSEPARATED FLUE GAS(8,1)\|UNDERLINED NUMERAL(7,3)\|STOICHIOMETRIC RATIO(6,4)\|ALKALINE INPUT(6,1)\|AMBIENT PRESSURE CARBONATION(6,1)\|ANTIGORITE(6,1)\|AQUEOUS PHASE CARBONATION(6,1)\|AQUEOUS REACTION(6,1)\|AUTOCLAVE(6,1)\|BOUND HYDROXIDE GROUP(6,1)\|BYPRODUCT(6,1)\|CHRYSOTILE(6,1)\|CLEAR BENEFIT(6,1)\|CO2 MASS(6,1)\|CO2 REMOVAL(6,1)\|CONCENTRATED SODIUM HYDROXIDE(6,1)\|CONCERN CAUSE(6,1)\|CONSUMPTION CONDITION(6,1)\|CONTAMINATION(6,1)\|DE CARBONIZED FLUE GAS(6,1)\|DIFFERENCE PLOT(6,1)\|DISCOVERY(6,1)\|DISSOLUTION DISINTEGRATION(6,1)\|ECONOMIC FEASIBILITY(6,1)\|EXCESS ALKALI(6,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(6,1)\|FIXED BED(6,1)\|\|(GB2516141)\|MAGNESIA(100,31)\|MAGNESIUM SILICATE(100,27)\|MAGNESIUM SILICATE MINERAL(100,10)\|UNPRESSURIZED VESSEL(100,5)\|ACTIVATION(100,2)\|INEFFICIENCY(97,2)\|SHELL INTERNATIONAL(73,1)\|MINERAL CARBONATION(69,4)\|DRY POWDER(67,4)\|ENERGY WASTAGE(63,1)\|MAGNESIUM SILICATE DRY POWDER(60,2)\|INDIRECT SEQUESTRATION(56,1)\|METAL MINERAL SILICATE DIGESTION(56,1)\|ALKALINE AQUEOUS LIQUID SLURRY(54,2)\|METHANEDIONE(53,37)\|ROCK(50,1)\|MOLAR RATIO(48,4)\|METHANEDIONE SEQUESTRATION(37,4)\|METALLIC MINERAL SILICATE(36,1)\|DISSOLUTION(34,8)\|AQUEOUS SOLUTION(33,13)\|INDUSTRIAL PLANT(32,1)\|MINERAL SILICATE(31,2)\|SODIUM CARBONATE(28,4)\|ALKALI METAL SILICATE(27,4)\|SOLID GLASS PRODUCT(24,4)\|FORSTERITE CAREFUL QUANTIFICATION(24,1)\|SERPENTINE FEEDSTOCK TONNE(24,1)\|FLUE GAS(22,23)\|GLASS PRODUCT(22,4)\|TEMPORAL DURATION(22,4)\|MINERAL FEEDSTOCK CARBONATION(22,1)\|ALKALI METAL HYDROXIDE(21,7)\|AQUEOUS PHASE PRODUCTION(20,2)\|ENERGY EFFICIENCY(20,1)\|SALABLE INDUSTRIAL FEEDSTOCK(20,1)\|ALKALI METAL(19,23)\|ALKALINE COMPOUND(18,6)\|BRUCITE CARBONATION(18,1)\|CONTEMPORARY RESEARCH OVERVIEW(18,1)\|MAGNESIA CARBONATION(18,1)\|MAGNESIA TONNE(18,1)\|METHANEDIONE TONNE(18,1)\|MINERAL CARBONATION SCIENCE(18,1)\|OLIVINE CARBONATION(18,1)\|SEQUESTRATING METHANEDIONE(18,1)\|SEQUESTRATION METHANEDIONE(18,1)\|UNPRESSURIZED AQUEOUS CARBONATION(18,1)\|BLENCOE ASSERTION(16,1)\|BRUCITE QUANTIFICATION(16,1)\|PREDOMINANTLY INSOLUBLE MINERAL PARTICLE(16,1)\|RIETVELD REFINEMENT QPA(16,1)\|SATISFACTORY MINERAL CARBONATION(16,1)\|SERPENTINE DEHYDROXYLATION(16,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(16,1)\|STEP CONDITION(16,1)\|MAGNESIUM SILICATE CONVERSION(14,3)\|OLIVINE POWDER(14,2)\|ANTHROPOGENIC OXIDATION(14,1)\|CARBONATION REACTOR(14,1)\|CO2 SCRUBBING(14,1)\|INTENSE PREPROCESSING(14,1)\|MAGNESIA DISSOLVE(14,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(14,1)\|MINERAL CARBONATION REACTION(14,1)\|MINERAL SEQUESTRATION(14,1)\|OLIVINE DIGESTION(14,1)\|PROPOSED MINERAL CARBONATION(14,1)\|SCALABILITY EXPERIMENT(14,1)\|CAUSTIC ALKALI METAL HYDROXIDE(12,4)\|WOLLASTONITE(12,4)\|BRUCITE DISPERSION(12,1)\|BRUCITE POWDER SEPARATION(12,1)\|CARBONACEOUS FOSSIL FUEL(12,1)\|CO2 TONNE(12,1)\|HUGE ENERGY PENALTY(12,1)\|MAGNESIA POWDER(12,1)\|MAGNESIUM SILICATE MINERAL DISSOLUTION(12,1)\|MASTER THESIS(12,1)\|METASTABLE CARBONATE(12,1)\|MINERALOGICAL SITE(12,1)\|MINING HIGH COST(12,1)\|SILICATE MINERAL CARBONATION(12,1)\|STIRRED TEFLON VESSEL(12,1)\|UTILIZATION OPTION(12,1)\|VESSEL PRESSURIZATION(12,1)\|EXPERIMENTAL PATTERN(11,2)\|INORGANIC POWDER(11,2)\|METHANEDIONE SOURCE(11,2)\|UNPRESSURIZED CONTINUOUS MODE(11,2)\|ALKALINE EARTH SILICATE(10,7)\|AMBIENT UNPRESSURIZED CONDITION(10,1)\|AQUEOUS MAGNESIA(10,1)\|BICARBONATE ION(10,1)\|CO2 TRANSPORT(10,1)\|DIGESTION VESSEL(10,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(10,1)\|MAGNESIUM SILICATE MINERAL POWDER(10,1)\|METAL SILICATE CARBONATION(10,1)\|MINERAL HYDROXIDE(10,1)\|PARTICLE ATTRITION(10,1)\|PRESSURIZATION DEPRESSURIZATION(10,1)\|SAMPLE XRD PATTERN(10,1)\|SLURRY CIRCULATION(10,1)\|SLURRY DROPLET SOLUTION(10,1)\|STABLE MINERAL CARBONATE(10,1)\|STOICHIOMETRIC CONVERSION(10,1)\|STOICHIOMETRIC MOLAR RATIO(10,1)\|WATER CARBONATION REACTION(10,1)\|AMBIENT ATMOSPHERIC PRESSURE(9,6)\|DIGESTION(9,5)\|ALKALI METAL BICARBONATE(8,4)\|ALKALI METAL CARBONATE(8,4)\|TEMPERATURE ELEVATION(8,4)\|HIGH COST(8,2)\|LITER WATER(8,2)\|MODEL CALCULATION(8,2)\|MOLALITY(8,2)\|PRODUCTION THROUGHPUT(8,2)\|SEAWATER(8,2)\|ABUNDANT SOURCE(8,1)\|ACIDIC PRETREATMENT(8,1)\|AGEING(8,1)\|ALKALI TREATMENT(8,1)\|ALKALINE PH(8,1)\|BRUCITE MAJOR PHASE(8,1)\|CALCIUM SILICATE MINERAL(8,1)\|CO2 EMISSION DISTANT SOURCE(8,1)\|CO2 EXPENSIVE SEPARATION(8,1)\|CO2 REACTION(8,1)\|CO2 SEQUESTRATION CAPACITY(8,1)\|DRY STOICHIOMETRIC REACTION(8,1)\|EARTH ATMOSPHERE(8,1)\|ELECTRICITY GENERATING FACILITY(8,1)\|FEED MINERAL(8,1)\|GEOLOGIC TIMESCALE(8,1)\|GLASS SOLIDIFICATION(8,1)\|HUGE SCALE(8,1)\|HYDROTHERMAL REACTION SAVE(8,1)\|INORGANIC PARTICLE(8,1)\|INTIAL(8,1)\|MAGNESIUM BICARBONATE MG(8,1)\|MAGNESIUM SILICATE CRYSTAL(8,1)\|MAGNESIUM SILICATE MINERAL DEPOSIT(8,1)\|MAGNESIUM SILICATE PARTICLE(8,1)\|MAGNESIUM SILICATE POWDER(8,1)\|MONITORED EXIT GAS(8,1)\|NATURALLY OCCURRING FEEDSTOCK(8,1)\|OLIVINE REACTION(8,1)\|PRIMARY INITIATIVE(8,1)\|QUANTITATIVE PHASE ANALYSIS(8,1)\|REACTION ACCELERATOR(8,1)\|REACTION SOLUBLE FRACTION(8,1)\|RELIANCE(8,1)\|SALABLE CHEMICAL(8,1)\|STIRRED BED(8,1)\|STIRRED REACTOR(8,1)\|UNPRESSURIZED REACTION VESSEL(8,1)\|UNSEPARATED FLUE GAS(8,1)\|UNDERLINED NUMERAL(7,3)\|STOICHIOMETRIC RATIO(6,4)\|ALKALINE INPUT(6,1)\|AMBIENT PRESSURE CARBONATION(6,1)\|ANTIGORITE(6,1)\|AQUEOUS PHASE CARBONATION(6,1)\|AQUEOUS REACTION(6,1)\|AUTOCLAVE(6,1)\|BOUND HYDROXIDE GROUP(6,1)\|BYPRODUCT(6,1)\|CHRYSOTILE(6,1)\|CLEAR BENEFIT(6,1)\|CO2 MASS(6,1)\|CO2 REMOVAL(6,1)\|CONCENTRATED SODIUM HYDROXIDE(6,1)\|CONCERN CAUSE(6,1)\|CONSUMPTION CONDITION(6,1)\|CONTAMINATION(6,1)\|DE CARBONIZED FLUE GAS(6,1)\|DIFFERENCE PLOT(6,1)\|DISCOVERY(6,1)\|DISSOLUTION DISINTEGRATION(6,1)\|ECONOMIC FEASIBILITY(6,1)\|EXCESS ALKALI(6,1)\|EXCESS SODIUM HYDROXIDE RECOVERY(6,1)\|FIXED BED(6,1)\|\|(GB2515995)\|METHANEDIONE(100,32)\|SEQUESTRATING METHANEDIONE(100,4)\|INEFFICIENCY(36,2)\|SHELL INTERNATIONALE(36,1)\|ALKALINE COMPOUND(35,10)\|SEQUESTRATION METHANEDIONE(30,2)\|BLEND CONTENT(26,1)\|MINERAL CARBONATION(24,5)\|BLEND(23,1)\|ENERGY WASTAGE(23,1)\|SCALABILITY(22,1)\|METHANEDIONE SOURCE(20,2)\|FLU GAS(20,1)\|INDIRECT SEQUESTRATION(20,1)\|REACTION CHAMBER(19,4)\|CO2(18,11)\|REACTION CHAMBER BLENDING CONTENT(18,1)\|SILICATE MATERIAL(17,6)\|BLENDING SYSTEM(17,1)\|ROCK(17,1)\|METAL MINERAL SILICATE DIGESTION(16,2)\|BICARBONATE(15,2)\|MINING(14,1)\|ALKALINE EARTH SILICATE(12,5)\|MOLALITY(11,2)\|INDUSTRIAL PLANT(11,1)\|LITER WATER(10,2)\|METALLIC MINERAL SILICATE(10,2)\|METHANEDIONE SEQUESTRATION(10,2)\|TEMPORAL DURATION(8,4)\|FORSTERITE CAREFUL QUANTIFICATION(8,1)\|SERPENTINE FEEDSTOCK TON(8,1)\|AQUEOUS SOLUTION(7,5)\|FLUE GAS(6,12)\|ALKALI METAL(6,5)\|AMBIENT ATMOSPHERIC PRESSURE(6,2)\|BRUCITE CARBONATION(6,1)\|CONTEMPORARY RESEARCH OVERVIEW(6,1)\|FOSSIL CARBONACEOUS FUEL(6,1)\|METHANEDIONE TONNE(6,1)\|MINERAL CARBONATION SCIENCE(6,1)\|OLIVINE CARBONATION(6,1)\|SEQUESTERING METHANEDIONE(6,1)\|ENERGY EFFICIENCY(5,3)\|STOICHIOMETRIC RATIO(5,3)\|BRUCITE QUANTIFICATION(5,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(5,1)\|MINERAL CARBONATION REACTION(5,1)\|MINERAL SEQUESTRATION(5,1)\|OLIVINE DIGESTION(5,1)\|RIETVELD REFINEMENT QPA(5,1)\|SATISFACTORY MINERAL CARBONATION(5,1)\|SCALABILITY EXPERIMENT(5,1)\|SERPENTINE DEHYDROXYLATION(5,1)\|SILICATE FEEDSTOCK ACID PRETREATMENT(5,1)\|DISSOLUTION(4,4)\|WOLLASTONITE(4,4)\|EXPERIMENTAL PATTERN(4,2)\|ANTHROPOGENIC OXIDATION(4,1)\|BRUCITE DISPERSION(4,1)\|BRUCITE POWDER SEPARATION(4,1)\|HUGE ENERGY PENALTY(4,1)\|MAGNESIA MG(4,1)\|MASTER THESIS(4,1)\|MINERALOGICAL SITE(4,1)\|STIRRED TEFLON VESSEL(4,1)\|UNPRESSURIZED VESSEL(4,1)\|DIGESTION(3,5)\|ALKALI METAL COMPOUND(3,2)\|EXCESS CONSUMPTION(3,2)\|GAS MIXTURE(3,2)\|HIGH COST(3,2)\|MODEL CALCULATION(3,2)\|PURE WATER VAPOR PRESSURE(3,2)\|DIGESTION VESSEL(3,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(3,1)\|METAL SILICATE CARBONATION(3,1)\|MINERAL HYDROXIDE(3,1)\|SAMPLE XRD PATTERN(3,1)\|STABLE MINERAL CARBONATE(3,1)\|STOICHIOMETRIC MOLAR RATIO(3,1)\|SILICON MONOXIDE(2,9)\|UNDERLINED NUMERAL(2,3)\|ABUNDANT SOURCE(2,1)\|ACIDIC PRETREATMENT(2,1)\|ADAPTABILITY(2,1)\|ALKALI TREATMENT(2,1)\|ALKALINE COMPOUND INPUT(2,1)\|ALKALINE COMPOUND SODIUM HYDROXIDE(2,1)\|AUTOCLAVE(2,1)\|CALCIUM SILICATE MINERAL(2,1)\|CONCENTRATED SODIUM HYDROXIDE(2,1)\|CONCERN CAUSE(2,1)\|DE CARBONIZED FLUE GAS(2,1)\|DIFFERENCE PLOT(2,1)\|DISCOVERY(2,1)\|EARTH ATMOSPHERE(2,1)\|ECONOMIC FEASIBILITY(2,1)\|ELECTRICITY(2,1)\|EXCESS ALKALI(2,1)\|FEED MINERAL(2,1)\|GENERATING FACILITY(2,1)\|GEOLOGIC TIMESCALE(2,1)\|GOVERNMENT(2,1)\|HYDROTHERMAL REACTION SAVE(2,1)\|INCREASING RELIANCE(2,1)\|INSTRUMENTALITY(2,1)\|MAGNESIUM BEARING MINERAL(2,1)\|MAGNESIUM BICARBONATE MG(2,1)\|MAGNESIUM SILICATE CONVERSION(2,1)\|NATURALLY OCCURRING FEEDSTOCK(2,1)\|NONEXCLUSIVE(2,1)\|OLIVINE REACTION(2,1)\|PRIMARY INITIATIVE(2,1)\|QUANTITATIVE PHASE ANALYSIS(2,1)\|REACTION ACCELERATOR(2,1)\|REACTION SOLUBLE FRACTION(2,1)\|STIRRED REACTOR(2,1)\|UNSEPARATED FLUE GAS(2,1)\|\|(CN106573197)\|MAGNESIUM SILICATE(100,40)\|MAGNESIA(100,32)\|ACTIVATED SILICATE MINERAL(100,1)\|NONCLOSED NONPRESSURIZED CONTAINER(100,1)\|ALKALINE SLURRY(63,3)\|MIXING MAGNESIA(53,1)\|MINERAL SUBSTANCE CARBONATION(51,1)\|MAGNESIUM SILICATE ROCK(37,2)\|METHANEDIONE GAS(34,24)\|ALKALI METAL SILICATE(25,5)\|ELEMENTAL SILICON(25,1)\|DRIED ALKALI METAL HYDROXIDE(21,1)\|GLASS PHASE(20,2)\|GLASSY PHASE(20,1)\|ALKALI METAL HYDROXIDE(19,7)\|DRIED ALKALI METAL(17,1)\|SUSPENDED BRUCITE PARTICLE(15,4)\|NONSEALED NONPRESSURIZED CONTAINER(15,2)\|ALKALI METAL(14,21)\|SOLID PHASE(13,4)\|METHANEDIONE GAS SCRUBBING(12,2)\|MABELL DELGADO TORR SIE(12,1)\|MINERAL CARBONATION SCIENCE ASSESSMENT(12,1)\|INTERMEDIATE PRODUCT(11,1)\|METHANEDIONE REMOVAL(10,4)\|BRUCITE CARBONATION(10,1)\|SILICATE FEEDSTOCK TON(10,1)\|SILICATE ORE FEEDSTOCK(10,1)\|METHANEDIONE SEQUESTRATION(9,5)\|POTASSIUM HYDROXIDE(9,3)\|DGC REACTOR(9,2)\|MAGNESIA POWDER(9,2)\|DUNITE ALKALINE DIGESTION(9,1)\|METHANEDIONE SCRUBBING(9,1)\|METHANEDIONE SEQUESTRATION CAPACITY(9,1)\|METHANEDIONE TON(9,1)\|OLIVINE CARBONATION(9,1)\|TECHNOLOGY SWISS FEDERAL INSTITUTE(9,1)\|INLET METHANEDIONE(8,2)\|CO2ABSOLUTE UNCERTAINTY(8,1)\|MAGNESIA TON(8,1)\|METHANEDIONE DISSOLUTION(8,1)\|METHANEDIONE VOLUMETRIC CAPACITY(8,1)\|PURITY OLIVINE MIXING(8,1)\|CELSIUS(7,11)\|DUNITE MOLAR RATIO(7,2)\|OLIVINE POWDER(7,2)\|SILICATE RAW MATERIAL(7,2)\|THERMOGRAVIMETRIC ANALYSIS(7,2)\|ATMOSPHERIC METHANEDIONE(7,1)\|BICARBONATE ION HCO(7,1)\|BRUCITE SOLUBILITY(7,1)\|CARBONATOR REACTOR(7,1)\|DOWNFLOW GAS CONTACTOR(7,1)\|FOSSIL ENERGY TON(7,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(7,1)\|METHANEDIONE GAS TON(7,1)\|METHANEDIONE GAS TRANSPORTATION(7,1)\|MOIST BRUCITE(7,1)\|OLIVINE DIGESTION(7,1)\|OLIVINE DISSOLUTION REACTION(7,1)\|OLIVINE FEEDSTOCK(7,1)\|OLIVINE MINING(7,1)\|SILICATE CARBONATION REACTION(7,1)\|SOCIAL ATTENTION(7,1)\|FLUE GAS(6,23)\|FORSTERITE(6,4)\|WOLLASTONITE(6,4)\|CARBONATING(6,2)\|ENERGY EFFICIENCY(6,2)\|MAGNESIUM ION(6,2)\|ABUNDANT MINERAL YIELD(6,1)\|BRUCITE DISPERSION(6,1)\|BRUCITE UTILIZATION(6,1)\|CARBONATE BYPRODUCT(6,1)\|CONTEMPORARY RESEARCH(6,1)\|CRYSTALLINE MAGNESIA LAYER(6,1)\|ECONOMIC VIABILITY(6,1)\|GENERAL CONSUMPTION(6,1)\|MAGNESIA CONVERSION(6,1)\|MAGNESIUM MINERAL CARBONATE(6,1)\|MAGNESIUM SILICATE ORE POWDER(6,1)\|METHANEDIONE LEAVE(6,1)\|NONPRESSURIZED VESSEL(6,1)\|OVERNIGHT STOPPAGE(6,1)\|SEAWATER SYNTHESIS(6,1)\|SOLID MATERIAL(6,1)\|SULFUR DIOXIDE SEQUESTRATION(6,1)\|ULTRAMAFIC ROCK RICH(6,1)\|AMBIENT ATMOSPHERIC PRESSURE(5,6)\|OUTLET GAS(5,4)\|BASIC COMPOUND(5,3)\|REACTION VESSEL PRESSURIZATION(5,3)\|LIQUID PHASE REACTION(5,2)\|ACTIVATED SILICATE(5,1)\|ALKALINE REAGENT(5,1)\|AMBIENT NONPRESSURIZED CONDITION(5,1)\|ARTOCARPUS DISSOLUTION(5,1)\|BRUCITE LIQUID SUSPENSION(5,1)\|BRUCITE QUANTITATIVE ANALYSIS(5,1)\|BRUCITE REACTION(5,1)\|CARBON DIOXIDE MINERAL SEQUESTRATION(5,1)\|CARBONATE PRECIPITATE(5,1)\|CARBONATION REACTION EQUATION(5,1)\|CARRYING OUT METHANEDIONE(5,1)\|CRUDE OIL WORLDWIDE CONSUMPTION(5,1)\|INLET GAS METHANEDIONE(5,1)\|INORGANIC PARTICLE COLUMN(5,1)\|MAGNESIA FORMATION(5,1)\|MAGNESIA YIELD(5,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(5,1)\|MAGNESIUM SILICATE DECOMPOSITION(5,1)\|MAGNESIUM SILICATE DISSOLUTION(5,1)\|METAL SILICATE CARBONATION(5,1)\|METHANEDIONE EMISSION SOURCE(5,1)\|METHANEDIONE GAS SEPARATION(5,1)\|METHANEDIONE MASS(5,1)\|METHANEDIONE REACTION(5,1)\|METHANEDIONE SEQUESTRATION AREA(5,1)\|MINED MAGNESIUM SILICATE(5,1)\|MINERAL DIGESTION(5,1)\|MINERAL DISSOLUTION(5,1)\|OLIVINE CONVERSION(5,1)\|OLIVINE REACTION(5,1)\|PREMIXING CYLINDER(5,1)\|PRESSURE COMPACTED DUNITE POWDER(5,1)\|PRIMARY INSOLUBLE MINERAL PARTICLE(5,1)\|SEQUESTRATION QUALITY(5,1)\|SHELL INTERNATIONAL(5,1)\|SILICATE MINERAL ACTIVATION(5,1)\|SLURRY CIRCULATION(5,1)\|SODIUM HYDROXIDE CONCENTRATIONS2THE(5,1)\|STACKING SITE(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|VALUABLE MINERAL(5,1)\|WIDESPREAD ATTENTION(5,1)\|BLENCOE(4,5)\|ACADEMIA(4,2)\|METHANEDIONE SEQUESTRATION REACTION(4,2)\|MG2SIO(4,2)\|MINERAL CARBONATION(4,2)\|ALKALINE COMPOUND(4,1)\|ALKALINE LIQUID SLURRY(4,1)\|ALKALINE PH(4,1)\|ALKALINE WASTE(4,1)\|AMBIENT ATMOSPHERE(4,1)\|AQUEOUS MAGNESIA SOLUTION(4,1)\|BRUCITE CONTENT(4,1)\|BUBBLE COLUMN(4,1)\|CHEMICAL THERMODYNAMIC VIEWPOINT(4,1)\|CURVING PROFILE(4,1)\|EARTH ATMOSPHERE(4,1)\|EXTENSIBILITY(4,1)\|FAVORABLE REACTION(4,1)\|FEED MINERAL(4,1)\|GAS STREAMIN(4,1)\|INORGANIC POWDER(4,1)\|MAGNESIA AQUEOUS SUSPENSION(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MEASURED METHANEDIONE(4,1)\|METAL SILICATE CATION(4,1)\|METHANEDIONE GAS VOLUME(4,1)\|NATURALLY OCCURRING FEEDSTOCK(4,1)\|NONAUTOCLAVE CONDITION(4,1)\|NONEXCLUSIVE(4,1)\|NONLIQUID(4,1)\|PASSIVATING SOLID(4,1)\|PRACTICABILITY(4,1)\|PRESSURIZATION DEPRESSURIZATION(4,1)\|PRESSURIZED CLOSED VESSEL(4,1)\|PRESSURIZED EQUIPMENT(4,1)\|PRESSURIZED REACTION(4,1)\|SALABLE CHEMICAL(4,1)\|SCREENED SAMPLE(4,1)\|SEALED CONTAINER(4,1)\|SILICATE POWDER(4,1)\|SILICON DOSE MOLAR RATIO(4,1)\|SOLID BRUCITE MG(4,1)\|SOLUBLE COMPOUND(4,1)\|STIRRED BED(4,1)\|STIRRED REACTOR(4,1)\|TEFLON VESSEL(4,1)\|THREATENING(4,1)\|MGCO(3,3)\|PURIFICATION(3,2)\|ACCESSORY(3,1)\|ACIDIC REAGENT(3,1)\|AGING(3,1)\|ALKALI TREATMENT(3,1)\|ALKALINE DIGESTION(3,1)\|ALKALINE SOLUTION(3,1)\|ANTIGORITE(3,1)\|BONDED HYDROXIDE GROUP(3,1)\|CALCIUM MAGNESIUM SILICATE MINERAL(3,1)\|CAPNOMETER(3,1)\|CARBON DIOXIDE REMOVAL(3,1)\|CARBONACEOUS FOSSIL ENERGY SOURCE(3,1)\|CARBONATION TECHNICAL DETAIL(3,1)\|CHRYSOTILE(3,1)\|CLINOCHLOREITE(3,1)\|COMMENT(3,1)\|CONCENTRATED SODIUM HYDROXIDE(3,1)\|CORROSIVITY(3,1)\|DIFFERENCE CURVE(3,1)\|DIGESTION REACTION VESSEL(3,1)\|ENERGY LOSS(3,1)\|ENSTATITE(3,1)\|EXENDIN(3,1)\|EXPERIMENTAL PERIOD(3,1)\|FIXED BED(3,1)\|GEOLOGY(3,1)\|GLASS TUBE ROTAMETER(3,1)\|GOVERNMENT(3,1)\|H2O RATIO(3,1)\|INFINITY(3,1)\|MAGNESIUM BICARBONATE AQUEOUS SOLUTION(3,1)\|\|(CN106573197)\|MAGNESIUM SILICATE(100,41)\|MAGNESIA(100,34)\|ACTIVATED SILICATE MINERAL(100,1)\|NONSEALED PRESSURIZED CONTAINER(100,1)\|ALKALINE SLURRY(79,2)\|METHANEDIONE SEQUESTRATION(69,16)\|MINERAL SUBSTANCE CARBONATION(69,1)\|MAGNESIA GLASS PHASE(60,1)\|MAGNESIUM SILICATE ROCK(50,2)\|METHANEDIONE GAS(45,24)\|ALKALI METAL SILICATE(34,5)\|GLASS PHASE(27,2)\|GLASSY PHASE(27,1)\|SUSPENDED BRUCITE PARTICLE(20,4)\|NONSEALED NONPRESSURIZED CONTAINER(20,2)\|SOLID PHASE(18,4)\|MABELL DELGADO TORR SIE(17,1)\|MINERAL CARBONATION SCIENCE ASSESSMENT(17,1)\|METHANEDIONE GAS SCRUBBING(16,2)\|INTERMEDIATE PRODUCT(15,1)\|METHANEDIONE REMOVAL(14,4)\|BRUCITE CARBONATION(14,1)\|DRIED ALKALI METAL COMPOUND(14,1)\|SILICATE FEEDSTOCK TON(14,1)\|SILICATE ORE FEEDSTOCK(14,1)\|DUNITE ALKALINE DIGESTION(13,1)\|METHANEDIONE SCRUBBING(13,1)\|METHANEDIONE SEQUESTRATION CAPACITY(13,1)\|METHANEDIONE TON(13,1)\|OLIVINE CARBONATION(13,1)\|TECHNOLOGY SWISS FEDERAL INSTITUTE(13,1)\|METHANEDIONE SEQUESTRATION(12,5)\|POTASSIUM CARBONATE(12,3)\|POTASSIUM HYDROXIDE(12,3)\|DGC REACTOR(12,2)\|MAGNESIA POWDER(12,2)\|SODIUM CARBONATE(11,3)\|INLET METHANEDIONE(11,2)\|CO2ABSOLUTE UNCERTAINTY(11,1)\|MAGNESIA TON(11,1)\|METHANEDIONE DISSOLUTION(11,1)\|METHANEDIONE VOLUMETRIC CAPACITY(11,1)\|PURITY OLIVINE MIXING(11,1)\|DUNITE MOLAR RATIO(10,2)\|OLIVINE POWDER(10,2)\|SILICATE RAW MATERIAL(10,2)\|THERMOGRAVIMETRIC ANALYSIS(10,2)\|ATMOSPHERIC METHANEDIONE(10,1)\|BICARBONATE ION HCO(10,1)\|BRUCITE SOLUBILITY(10,1)\|CARBONATOR REACTOR(10,1)\|DOWNFLOW GAS CONTACTOR(10,1)\|FOSSIL ENERGY TON(10,1)\|MAGNESIUM SILICATE MINERAL FEEDSTOCK(10,1)\|METHANEDIONE GAS TON(10,1)\|METHANEDIONE GAS TRANSPORTATION(10,1)\|MOIST BRUCITE(10,1)\|OLIVINE DIGESTION(10,1)\|OLIVINE DISSOLUTION REACTION(10,1)\|OLIVINE FEEDSTOCK(10,1)\|OLIVINE MINING(10,1)\|SILICATE CARBONATION REACTION(10,1)\|SOCIAL ATTENTION(10,1)\|FLUE GAS(9,23)\|REACTION TEMPERATURE(9,10)\|ENERGY EFFICIENCY(9,2)\|MAGNESIUM ION(9,2)\|CELSIUS(8,9)\|FORSTERITE(8,4)\|WOLLASTONITE(8,4)\|CARBONATING(8,2)\|ABUNDANT MINERAL YIELD(8,1)\|BRUCITE DISPERSION(8,1)\|BRUCITE UTILIZATION(8,1)\|CARBONATE BYPRODUCT(8,1)\|CONTEMPORARY RESEARCH(8,1)\|CRYSTALLINE MAGNESIA LAYER(8,1)\|ECONOMIC VIABILITY(8,1)\|GENERAL CONSUMPTION(8,1)\|MAGNESIA CONVERSION(8,1)\|MAGNESIUM MINERAL CARBONATE(8,1)\|MAGNESIUM SILICATE ORE POWDER(8,1)\|METHANEDIONE LEAVE(8,1)\|NONPRESSURIZED VESSEL(8,1)\|OVERNIGHT STOPPAGE(8,1)\|SEAWATER SYNTHESIS(8,1)\|SOLID MATERIAL(8,1)\|SULFUR DIOXIDE SEQUESTRATION(8,1)\|ULTRAMAFIC ROCK RICH(8,1)\|AMBIENT ATMOSPHERIC PRESSURE(7,6)\|OUTLET GAS(7,4)\|BASIC COMPOUND(7,3)\|REACTION VESSEL PRESSURIZATION(7,3)\|LIQUID PHASE REACTION(7,2)\|ACTIVATED SILICATE(7,1)\|ALKALINE REAGENT(7,1)\|AMBIENT NONPRESSURIZED CONDITION(7,1)\|ARTOCARPUS DISSOLUTION(7,1)\|BRUCITE LIQUID SUSPENSION(7,1)\|BRUCITE QUANTITATIVE ANALYSIS(7,1)\|BRUCITE REACTION(7,1)\|CARBON DIOXIDE MINERAL SEQUESTRATION(7,1)\|CARBONATE PRECIPITATE(7,1)\|CARBONATION REACTION EQUATION(7,1)\|CARRYING OUT METHANEDIONE(7,1)\|CRUDE OIL WORLDWIDE CONSUMPTION(7,1)\|INLET GAS METHANEDIONE(7,1)\|INORGANIC PARTICLE COLUMN(7,1)\|MAGNESIA FORMATION(7,1)\|MAGNESIA YIELD(7,1)\|MAGNESIUM MINERAL SILICATE CONVERSION(7,1)\|MAGNESIUM SILICATE DECOMPOSITION(7,1)\|MAGNESIUM SILICATE DISSOLUTION(7,1)\|METAL SILICATE CARBONATION(7,1)\|METHANEDIONE EMISSION SOURCE(7,1)\|METHANEDIONE GAS SEPARATION(7,1)\|METHANEDIONE MASS(7,1)\|METHANEDIONE REACTION(7,1)\|METHANEDIONE SEQUESTRATION AREA(7,1)\|MINED MAGNESIUM SILICATE(7,1)\|MINERAL DIGESTION(7,1)\|MINERAL DISSOLUTION(7,1)\|OLIVINE CONVERSION(7,1)\|OLIVINE REACTION(7,1)\|PREMIXING CYLINDER(7,1)\|PRESSURE COMPACTED DUNITE POWDER(7,1)\|PRIMARY INSOLUBLE MINERAL PARTICLE(7,1)\|SEQUESTRATION QUALITY(7,1)\|SHELL INTERNATIONAL(7,1)\|SILICATE MINERAL ACTIVATION(7,1)\|SLURRY CIRCULATION(7,1)\|SODIUM HYDROXIDE CONCENTRATIONS2THE(7,1)\|STACKING SITE(7,1)\|STOICHIOMETRIC PROPORTION(7,1)\|VALUABLE MINERAL(7,1)\|WIDESPREAD ATTENTION(7,1)\|BLENCOE(6,5)\|ACADEMIA(6,2)\|METHANEDIONE SEQUESTRATION REACTION(6,2)\|MG2SIO(6,2)\|MINERAL CARBONATION(6,2)\|REACTION PRODUCT MAGNESIA CONTENT(6,2)\|MGCO(5,3)\|PURIFICATION(5,2)\|ALKALINE COMPOUND(5,1)\|ALKALINE LIQUID SLURRY(5,1)\|ALKALINE PH(5,1)\|ALKALINE WASTE(5,1)\|AMBIENT ATMOSPHERE(5,1)\|AQUEOUS MAGNESIA SOLUTION(5,1)\|BRUCITE CONTENT(5,1)\|BUBBLE COLUMN(5,1)\|CHEMICAL THERMODYNAMIC VIEWPOINT(5,1)\|CURVING PROFILE(5,1)\|EARTH ATMOSPHERE(5,1)\|EXTENSIBILITY(5,1)\|FAVORABLE REACTION(5,1)\|FEED MINERAL(5,1)\|GAS STANDARD ATMOSPHERIC PRESSURE(5,1)\|INORGANIC POWDER(5,1)\|MAGNESIA AQUEOUS SUSPENSION(5,1)\|MAGNESIUM SILICATE CONVERSION(5,1)\|MEASURED METHANEDIONE(5,1)\|METAL SILICATE CATION(5,1)\|METHANEDIONE GAS VOLUME(5,1)\|NATURALLY OCCURRING FEEDSTOCK(5,1)\|NONAUTOCLAVE CONDITION(5,1)\|NONEXCLUSIVE(5,1)\|NONLIQUID(5,1)\|PASSIVATING SOLID(5,1)\|PRACTICABILITY(5,1)\|PRESSURIZATION DEPRESSURIZATION(5,1)\|PRESSURIZED CLOSED VESSEL(5,1)\|PRESSURIZED EQUIPMENT(5,1)\|PRESSURIZED REACTION(5,1)\|SALABLE CHEMICAL(5,1)\|SCREENED SAMPLE(5,1)\|SEALED CONTAINER(5,1)\|SILICATE POWDER(5,1)\|SILICON DOSE MOLAR RATIO(5,1)\|SOLID BRUCITE MG(5,1)\|SOLUBLE COMPOUND(5,1)\|STIRRED BED(5,1)\|STIRRED REACTOR(5,1)\|TEFLON VESSEL(5,1)\|THREATENING(5,1)\|ALKALI METAL COMPOUND(4,11)\|ACCESSORY(4,1)\|ACIDIC REAGENT(4,1)\|AGING(4,1)\|ALKALI TREATMENT(4,1)\|ALKALINE DIGESTION(4,1)\|ALKALINE SOLUTION(4,1)\|ANTIGORITE(4,1)\|BONDED HYDROXIDE GROUP(4,1)\|CALCIUM MAGNESIUM SILICATE MINERAL(4,1)\|CAPNOMETER(4,1)\|CARBON DIOXIDE REMOVAL(4,1)\|CARBONACEOUS FOSSIL ENERGY SOURCE(4,1)\|CARBONATION TECHNICAL DETAIL(4,1)\|CHRYSOTILE(4,1)\|CLINOCHLOREITE(4,1)\|COMMENT(4,1)\|CONCENTRATED SODIUM HYDROXIDE(4,1)\|CORROSIVITY(4,1)\|DIFFERENCE CURVE(4,1)\|DIGESTION REACTION VESSEL(4,1)\|ENERGY LOSS(4,1)\|ENSTATITE(4,1)\|EXENDIN(4,1)\|EXPERIMENTAL PERIOD(4,1)\|FIXED BED(4,1)\|GEOLOGY(4,1)\|GLASS TUBE ROTAMETER(4,1)\|	(EP3129125)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising:\| a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from the group consisting of alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture;\| b. heating the dry solid-solid mixture to a temperature below 300 °C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and\| c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|2. A method as claimed in claim 1, characterized in that the liquid slurry of step c is separated into solid and aqueous solution phase products.\|3. A method as claimed in claim 1 or 2, characterized in that the method includes reacting any of the aqueous phases at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|4. A method as claimed in claim 2, characterized in that the method includes mixing the solid phase product with water and reacted at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|5. A method as claimed in claim 3 or 4, characterized in that the method includes air as the gas in the reaction.\|6. A method as claimed in claim 3 or 4, characterized in that the method includes an industrial flue gas in the reaction.\|7. A method as claimed in claim 1, characterized in that the method includes using a hydroxide or a carbonate of sodium or a potassium as the alkali metal compound in the reaction.\|8. A method as claimed in claim 1, characterized in that the method includes a serpentine or an olivine rock as the magnesium silicate mineral in the reaction.\|9. A method as claimed in claim 1, characterized in that the method includes heating the unpressurised vessel in step (b) to a temperature in the range 140C-220C.\|10. A method as claimed in claims 1, characterized in that the method includes continuously adding the magnesium silicate mineral and alkali metal compound of step (a) together allowing continuous reacting thereof under the conditions of step (b) and further continuously removing the product of step (b).\|11. A method as claimed in claim 1, characterized in that the method includes the molar ratio of substantially 2 moles of alkali metal per mole of silicon in the mixture.	(EP3129125)\|TECHNICAL FIELD\|[0001] The present disclosure relates to methods of producing activated mineral silicate for use in sequestrating Carbon Dioxide, for example from flue-gas, by utilizing a process which involves digestion of metal mineral Silicates. Moreover, the present disclosure also relates to systems for executing aforesaid methods.\|BACKGROUND\|[0002] Increasing concentrations of Carbon Dioxide (CO2) in the Earth's atmosphere have recently caused concerns, as the present concentrations are substantial at 400 p.p.m. and increasing at a rate of 4 p.p.m. per annum. A major factor contributing to such increase is the anthropogenic oxidation of carbonaceous fossil fuels, for example coal, oil and gas. The World presently consumes circa 100 million barrels of oil per day.\|[0003] There have been recent initiatives to employ more renewable energy systems, for example wind turbines and tidal power generating systems, as well as sequestration of Carbon Dioxide (CO2) from flue-gases emitted from coal burning electricity generating facilities. Thus, primary initiatives involve utilizing energy efficient technologies, increasing reliance on renewable sources, and developing technologies for long term storage of Carbon Dioxide (CO2) emissions. The latter technology field is known as Carbon Dioxide (CO2) sequestration.\|[0004] There have been significant developments in Carbon Dioxide (CO2) sequestration in recent years, and Carbon Dioxide sequestration technologies have aroused considerable interest among governments, industries and scientific communities. Earlier methods of Carbon Dioxide (CO2) sequestration suffered from various drawbacks such as risk of water contamination, and a lack of suitable storage spaces for receiving sequestrated Carbon Dioxide (CO2); these drawbacks are familiar to a person skilled in the art.\|[0005] There has been considerable interest in mineral Carbonation technologies to address aforementioned problems associated with known Carbon Dioxide (CO2) sequestration. The Masters thesis by Mabell Delgado Torróntegui at ETH in Switzerland, "Assessing the Mineral carbonation science and technology" (2010), provides an overview of contemporary research in this field of Carbon Dioxide (CO2) sequestration technology. A key principle of mineral Carbonation is also known as "mineral sequestration technology", wherein sequestration of Carbon Dioxide (CO2) is achieved by capturing Carbon Dioxide (CO2) in a form of stable mineral Carbonates. Such sequestration employs a process which is an exothermic reaction of a metal Oxide and Carbon Dioxide (CO2) to form stable Carbonate materials as provided in a reaction formula (1):\| MO + CO2 => MCO3 + Heat (1)\|wherein M is a metal, preferably an alkaline earth metal such as Calcium or Magnesium.\|[0006] Most suitable and naturally abundant sources of these metal Oxides are Magnesium or Calcium Silicate minerals such as Olivine, wollastonite, and Serpentine. The Carbonation reactions of these minerals are as follows:\| Olivine:\| Mg2SiO4 + 2CO2 => 2MgCO3 + SiO2 + 89 kJ mol-1CO2 (2)\| Serpentine:\| Mg3Si2O3(OH)4 + 3CO2 => 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol-1CO2\| Wollastonite:\| CaSiO3 + CO2 => CaCO3 + SiO2 + 90 kJ mol-1CO2 (4)\|[0007] Although the above reactions (2) to (4) are thermodynamically favourable, the reactions in nature have, however, relatively slow reaction rates in a geologic time scale, and are unsuitable for industrial processes. Efforts have been made to try to accelerate these reactions. However, the efforts suffer from various limitations, such as energy wastage and a high cost of mining and transporting large amounts of rock, as well as industrial and environmental inefficiencies. Moreover, the mineral Silicates are not easily obtainable in suitable quantities and formats for allowing satisfactory mineral Carbonation to be achieved.\|[0008] In a published US patent no. US7604787B2 (MAROTO-VALER), "Process for sequestering Carbon Dioxide and Sulphur Dioxide", there is described a method of reacting a Silicate-based material with an acid to form a suspension, which is then combined with Carbon Dioxide to produce a metal salt, silica and regenerating acid in solution. This method has drawbacks of being environmentally harsh and inefficient. Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for removal and Capture of Carbon Dioxide from Flue Gases".\|[0009] Although, the prior art disclosures have been able to address some of the problems of mineral Carbonation through their indirect sequestration processes, there are several remaining problems which have not yet been resolved. Such remaining problems pertain to industrial scalability, environmental efficiency, and cost.\|[0010] Lately, research effort has focused upon Carbon Dioxide (CO2) sequestration by 'direct' Carbonation of Olivine or Serpentine. In these recent methods, Carbon Dioxide (CO2) is sequestered without acid pretreatment of Silicate feedstock. An Olivine reaction is:\| Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 (5)\|[0011] Moreover, for Serpentine, a corresponding reaction is:\| Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O (6)\|[0012] Experiments to determine the kinetics of these reactions (5) and (6) have shown that such reactions also suffer from poor energy efficiency and a high cost when up-scaled to an industrial plant. In order to accelerate the reactions (5) and (6), high temperatures in a range of 600°C to 650 °C are required. In a fuel-fired industrial power plant, attainment of such high temperatures would translate to a requirement of approximately 200 kW-h of electricity per tonne of Serpentine feedstock. Moreover, with a fossil fuel containing 1 tonne of Carbon, nearly 3.7 tonnes of Carbon Dioxide (CO2) is produced. Each tonne of Carbon Dioxide (CO2) consumes more than 2 tonnes of Serpentine during Carbonation. Combined with a pre-capture step to separate and pressurise CO2 from flue gas, the power required for Serpentine dehydroxylation Is around 20-30% of total power output from such fuel-fired industrial power plant. All these considerations lead to a huge energy penalty threatening the economic feasibility of this sequestration process.\|[0013] In a published US patent no. US8114374B2 (BLENCOE), "Carbonation of metal Silicates for long-term CO2 sequestration", there is described a method (hereinafter "Blencoe's method") of reacting a Silicate with an alkali metal hydroxide in an aqueous solution. The reaction with Carbon Dioxide (CO2) is then used to carbonate the metal formerly contained in the metal Silicate. This method has drawbacks of inefficiencies and poor overall Carbon capture properties. Blencoe's method comprises three steps:\| (1) reacting a metal silicate with a caustic alkali-metal hydroxide to produce a hydroxide of the metal formerly contained in the silicate;\| (2) reacting carbon dioxide with at least one of a caustic alkali-metal hydroxide and an alkali-metal silicate to produce at least one of an alkali-metal carbonate and an alkali-metal bicarbonate; and\| (3) reacting the metal hydroxide product of step (a) with at least one of the alkali-metal carbonate and the alkali-metal bicarbonate produced in step (b) to produce a carbonate of the metal formerly contained in the metal silicate of step (a).\|[0014] In Blencoe's first step (1), the alkali-metal hydroxide is in aqueous solution which limits the maximum reaction temperature to the vapour pressure of the aqueous solution at the pressure under which the reaction is carried out. A low reaction temperature limits the reaction rate at atmospheric pressure, while use of a pressurised vessel increases process costs. Alkali-metal hydroxides, such as NaOH and KOH, used in steps (1) and (2) are energy intensive and expensive chemicals to manufacture. In Blencoe's second step (1), alkali-metal hydroxide, additional to that used in step (1), is used to react with Carbon Dioxide. In Blencoe's second and third steps (2) and (3), an elevated pressure is required, namely having implied costs of a pressure vessel, in the range between the vapour pressure of water at the reaction temperature and Bar. It is doubtful that the overall process described is able to sequester more Carbon Dioxide as a metal carbonate than is generated as a consequence of manufacture of the alkali-metal hydroxides consumed in the process, or that the process is any cheaper to operate than Carbon Dioxide sequestration processes described in the prior art.\|[0015] Therefore, there is an urgent need to develop a process which is energy efficient, has a high throughput and is more cost effective than the prior art so that it can be used industrially.\|[0016] From the foregoing, it will be appreciated that the known methods of processing and the systems for mineral carbonation and Carbon Dioxide (CO2) sequestration, are neither optimal in their manner of operation nor adaptable to broader applications in a cost effective manner.\|SUMMARY\|[0017] The present invention seeks to provide an improved method of activation of magnesium silicate minerals by conversion to magnesium hydroxide.\|[0018] This present embodiment of the invention allows for a method of large scale industrial use and continuous carbonation without advanced pressure chambers or equipment.\|[0019] The present invention provides a method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, wherein the method comprises:\| a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from a group comprising alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture;\| b. heating the dry solid-solid mixture to a temperature below 300°C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and\| c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|[0020] Optionally, the method includes the liquid slurry of step c being separated into solid and aqueous solution phase products.\|[0021] Optionally, the method includes reacting any of the aqueous phases at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|[0022] Optionally, the method includes mixing the solid phase product with water and reacted at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|[0023] Optionally, the method includes air or flue gas as the gas in the reaction. This allows for a very simple and cost-effective solution utilizing what is available at the site of operation.\|[0024] Optionally, the method includes using a hydroxide or a carbonate of sodium or a potassium as the alkali metal compound in the reaction.\|[0025] Optionally, the method includes a serpentine or an olivine rock as the magnesium silicate mineral in the reaction. Further, optionally, the method includes heating the unpressurised vessel in step (b) to a temperature in the range 140 °C - 220 °C.\|[0026] Optionally, the method includes continuously adding the magnesium silicate mineral and alkali metal compound of step (a) together allowing continuous reacting thereof under the conditions of step (b) and further continuously removing the product of step (b).\|[0027] Optionally, the method includes the molar ratio of substantially 2 moles of alkali metal per mole of silicon in the mixture.\|[0028] Additional aspects, advantages, features and objects of the present invention would be made apparent from the drawings and the detailed description of the illustrative embodiments construed in conjunction with the appended claims that follow. It will be appreciated that features of the present invention are susceptible to being combined in various combinations from different embodiments without departing from the scope of the present invention as defined by the appended claims.\|DESCRIPTION OF DRAWINGS:\|[0029] The summary above, as well as the following detailed description of illustrative embodiments, is better understood when read in conjunction with the appended drawings. For the purpose of illustrating the present invention, exemplary constructions of the disclosure are shown in the drawings. However, the present invention is not limited to specific methods and apparatus disclosed herein. Moreover, those in the art will understand that the drawings are not to scale. Wherever possible, like elements have been indicated by identical numbers.\| FIG. 1 is an illustration of a flow chart of a digestion Step 1 involving alkaline digestion of Serpentine or Olivine to convert them to Brucite and Silica;\| FIG. 2 is an illustration of a flow chart of a Carbonation step 2 involving direct Carbonation of Brucite, namely Magnesium Hydroxide, with flue-gas to form Magnesium Carbonate;\| FIG.3a and 3b are illustrations of XRD patterns of selected samples, wherein solid products from dissolution of Dunite, namely a form of Olivine, using Sodium Hydroxide (NaOH) solution of concentration in a range of 15 to 40 mol/kg (left), and using Sodium Hydroxide (NaOH) solution of concentration 50 mol/kg (right) solutions. In the illustrations, following abbreviations are employed: Fo = Forsterite, Brc = Brucite, Clc = Clinochlore, En = Enstatite, Srp = Serpentine, Tlc = Talc, Spl = Spinel;\| FIG. 4a and 4b are illustrations of TG (4a) and DTG (4b) curves of selected samples: solid products from dissolution of Dunite at a temperature of 180°C for 15 for 6 hours with different concentrations of Sodium Hydroxide (NaOH) solution;\| FIG. 5 is a graph wherein there are shown Mg(OH)2 concentrations in solid products based on TG results: Dunite dissolved at a temperature of 180°C with different concentrations of Sodium Hydroxide (NaOH) solution, namely measured as moles of NaOH per kg of water. From the graph, it will be appreciated that the proportion of Dunite, namely magnesium silicate, converted to Brucite, namely magnesium hydroxide, increases approximately linearly with increase in NaOH concentration; extrapolation of this graph indicates that the proportion of Brucite in the solid product should approach 100% above a NaOH concentration >70mol/kg, namely equivalent to a NaOH: H2O ratio >1.26;\| FIG. 6 is an illustration of XRD patterns of solid products from dissolution of Dunite at 180 °C with Sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg solution, for different temporal durations;\| FIG. 7a and 7b are illustrations of TG (7a) and DTG (7b) curves of solid products from dissolution of Dunite at a temperature of 180° C with sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg for different temporal durations;\| FIG. 8 is a graph in which there is shown Magnesium Hydroxide Mg(OH)2 concentration in solid products based on TG results: Dunite dissolved at a temperature of 180 °C with a molar concentration of Sodium Hydroxide (NaOH) solution being 40 mol/kg for different durations;\| FIG. 9 is an illustration showing Rietveld Refinement QPA of raw Dunite, wherein: data points profile = experimental pattern; continue profile = calculated model (above); difference plot (below);\| FIG. 10 is an illustration showing Rietveld Refinement QPA of dissolved Dunite spiked with 10 wt% Silicon, wherein: data points profile = experimental pattern; continue profile = calculated model; and\| FIG. 11a and 11b are illustrations showing Brucite quantification with Rietveld Refinement and TGA (FIG. 11a), wherein Forsterite and Brucite concentrations were obtained via Rietveld Refinement QPA of selected samples (FIG. 11b).\| FIG. 12a and 12b depict experimental data concerning the removal of CO2 by means of Brucite powder in aqueous suspension, specifically the resulting CO2 level for a monitored exit gas after processing.\|[0030] In the accompanying drawings, an underlined number is employed to represent an item over which the underlined number is positioned or an item to which the underlined number is adjacent. A non-underlined number relates to an item identified by a line linking the non-underlined number to the item. When a number is non-underlined and accompanied by an associated arrow, the non-underlined number is used to identify a general item at which the arrow is pointing.\|DETAILED DESCRIPTION OF EMBODIMENTS\|[0031] The following detailed description illustrates embodiments of the present disclosure and ways in which they can be implemented.\|[0032] In FIG. 1, there is shown a digestion process 100, wherein there occurs alkaline digestion of a Silicate-based material, a naturally occurring feedstock containing magnesium or calcium silicate, such as Serpentine, Olivine, Dunite, and/or Wollastonite 101. The process 100 results in reaction products being generated, namely a conversion to Brucite and Silica in a case of Olivine 101 being a feed mineral employed. In the reaction, Olivine 101 is fed into a stirred reactor 102 together with an alkali 103 and heat is provided from a heat source 104. The alkali is beneficially selected from a mineral Hydroxide. Among the many metal Hydroxides that can find utility in this reaction, a preferable alkali used is Sodium Hydroxide (NaOH) .\|[0033] The reaction mixture of the digestion process 100 comprises a stoichiometric ratio between the soluble silicate based material and the solid hydroxide of the alkaline earth compound of about 1:2. This stoichiometric ratio aims to minimise the input of the alkaline compound, such as Sodium Hydroxide (NAOH), into the initial reaction mixture. This limits the regeneration of Sodium Hydroxide (NaOH) from carbonates at the end of the reaction, which is costly and time consuming. The reaction mixture is a dry mixture.\|[0034] According to a further embodiment, the reaction mixture is a solid-state dry mixture of a powder of the alkaline-earth silicate and the alkali-metal compound, in the stoichiometric ratio of one mole of silicon, namely in the silicate, per two moles of alkali-metal. Solid alkali-metal compounds, such as NaOH, KOH and Na2CO3, have high melting points, namely 318°C, 406°C and 851 °C, respectively. Using an aqueous system, such as taught by Blencoe, would therefore be expected to be essential to achieving mixing and reaction at temperatures below 300 °C. Surprisingly, in experiments using NaOH and Serpentine, namely magnesium silicate, it is found that a dry solid state mixture of the two rapidly melted, mixed and reacted to form magnesium hydroxide in an unpressurised vessel at temperatures as low as 180°C, namely well below the melting temperature of NaOH, namely 318°C, or of Serpentine, namely >1700 °C. Unlike Olivine, Serpentine has a crystal structure that contains chemically bound hydroxide groups, and it is believed that these groups may facilitate the dry stoichiometric reaction to form magnesium hydroxide.\|[0035] Dunite can also be used to yield Mg(OH)2 via solid state reaction, with a preferable ratio of Dunite to NaOH in a mole ratio of 1:2, at a temperature around 180 °C. Experiments conducted with a range of Dunite: NaOH mole ratios of 1:0.5, 1:1, 1:.5 and 1:2, where the powder has been formed into pellets by compaction with a hand press (3 tonnes for 1 minute for compression), returned results indicating a linear increase of Mg(OH)2 production with increase of NaOH, to a maximum weight percentage of Mg(OH)2 in the reaction products of around 46.7%. Reducing the amount of NaOH significantly lowered the extraction efficiency of the process.\|[0036] In contrast, results of non-inventive experiments, as provided in FIGs. 3a, 3b, 5, with aqueous NaOH and Olivine show that minimum reaction conditions of a temperature of 180°C and a NaOH concentration of 40mol/kg are substantially required to form magnesium hydroxide; this system requires a pressure vessel to reach a required reaction temperature.\|[0037] For the case of Dunite samples, comparison of the results cited above with alkaline digestion of Dunite with 50mol/kg NaOH aqueous system at 180°C under a similar time period, show that the yield of Mg(OH)2 via solid state reaction (55% to 62%) was on a par with that produced using the aqueous system (between 58% and 66%). The alkaline digestion with 50mol/kg NaOH required significantly more NaOH per 1 gram of Dunite processed such that the solid state reaction effected a 97% to 99% reduction of NaOH consumption. Additional experimental results comprising Dunite as a sample component are detailed later.\|[0038] Generally stated, it has been demonstrated that it is possible to extract Mg(OH)2 from magnesium containing silicate minerals via solid state reaction with NaOH and that the consumption of the alkaline reactant can be reduced, achieving significant yield of reaction. An additional advantage is the reduction of water consumption which would be needed for an aqueous process.\|[0039] Moreover, results have also shown, namely in FIG. 5, that without water, the NaOH concentration (mol/kg) effectively approaches infinity and might therefore be expected to approach 100% conversion of magnesium silicate to magnesium hydroxide. Compared to the aqueous reaction system, as exemplified by Blencoe, clear benefits of the non-aqueous dry-mixture and stoichiometric system using Serpentine are that:\| (i) no pressure vessel is required;\| (ii) melting and mixing surprisingly take place at 180 °C, to enable a rapid reaction at a rate similar to an aqueous system;\| (iii) a highest possible concentration and activity of NaOH is enabled, leading to a faster and more complete reaction than possible in an aqueous system at a similar temperature;\| (iv) the NaOH is totally consumed in a reaction with silicate to form solid sodium silicate, so that no subsequent process for recovery of excess NaOH from the reaction products is required;\| (v) Serpentine provides any water required for the stoichiometric conversion to magnesium hydroxide from its structural hydroxide groups, so that no free water needs to be added to the reaction system;\| (vi) the products of reaction, containing no excess NaOH, are a solidified glass which is substantially less caustic than in the aqueous process and are therefore much safer to handle;\| (vii) sodium silicate is readily separated from the products of reaction by dissolution and filtration, and is available without contamination by NaOH; and\| (viii) the process can be more readily and cheaply carried out at remote Serpentine or Olivine mine sites where water may not be available.\|[0040] Further, in the prior art of Blencoe it is described how the initial step (a) can be conducted at a pressure slightly below the vapour pressure of pure water for the temperature of that step. Blencoe does not claim a preferred temperature or pressure or aqueous solution composition for that initial step (a), but in a table of experimental results shows that all reactions in which serpentine or olivine are converted to a major phase of brucite are done in aqueous solution in a pressure vessel at a temperature of 200 °C and pressure <15atm. One experiment conducted at a temperature of 22 °C and 1atm pressure for 72hrs results in conversion to a minor phase of brucite; subsequent additional reaction at 200 °C and < 15bar then converts substantially to brucite with a minor residual phase of serpentine. Notwithstanding Blencoe's assertion of the technological and commercial advantage of avoiding pressure-intensifying equipment, at the effective reaction temperature of 200 °C for Blencoe's step (a), the vapour pressure of pure water is just above bar indicating that a pressure vessel must be used in this step. The current invention allows for the method and system to operate without expensive and complicated equipment used in Blencoe to operate at higher than atmospheric pressure.\|[0041] In the example of magnesium carbonates being produced according to the described method, a wide range of compounds including soluble magnesium bicarbonate Mg(HCO3)2 is produced in solution, but generates no separate water in the carbonation reaction:\| 2CO2+ Mg(OH)2 = Mg.(HCO3)2 (7)\|[0042] The preferred alkali 103 for this digestion process is beneficially Sodium Hydroxide or Potassium Hydroxide. It is also possible to use Sodium Carbonate, Sodium Bicarbonate, Potassium Carbonate and Potassium Bicarbonate as the alkali for the digestion process.\|[0043] The heat source 104 is employed to raise a temperature of the digestion process, whilst stirring of the mixture is implemented, to a temperature of less than 250 °C, and for a temporal period of less than 6 hours. A preferred range of temperature is from 140 °C to 220 °C. The reaction can be best performed with the temperature being less than 200 °C, and most preferentially at around 180 °C, throughout the process, as shown in the results FIG. 4 to FIG. 8. The digestion vessels used are most suitably Teflon (PTEE) to withstand hot-conc-NaOH with the maximum operating temperature usually specified at 220 °C. Experiments with Magnesium silicate mineral feedstocks have been showing excellent results for this process.\|[0044] This digestion process is preferably carried out at a pressure of less than Bar, wherein 1 Bar corresponds to nominal atmospheric pressure at sea-level. The reaction can be more preferably carried out at a pressure less than 10 Bar. The reaction can be furthermore preferably be carried out at pressure conditions lower than the vapour pressure of pure water at the temperature of reaction. The benefit of not having to use high pressure vessels to carry out hydrothermal reactions saves cost and also improves the applications of the technology in industrial applications at very high volumes and large scale installations.\|[0045] The process, after digestion of Olivine, is shown in equation 112. Here, the Brucite (MgOH2) 107, solid phase, is separated from a Silicate solution 108. Thereafter, the Silica precipitation process is carried out as depicted in the equations 113 and 112. The process, namely acid precipitation, can be carried out by adding either Carbon Dioxide (CO2) or acid 110. Excess alkali 111 is recovered and fed back to a chamber of the reactor 102. Performing the digestion process at ambient atmospheric pressure conditions avoids a need to employ equipment to increase pressure, for example an autoclave, and allows large scale, continuous sequestration of industrial Carbon Dioxide (CO2) emissions to be achieved. Avoiding the requirement for any pressurised containment of the reaction steps, provides several benefits:\| (i) much cheaper and simpler reaction vessels can be used;\| (ii) it is easier and cheaper to incorporate mixing, stirring and/or particle attrition to enhance reaction rates within an unpressurised reaction vessel;\| (iii) energy usage, namely energy wasted in pressurisation/ depressurisation, is lower;\| (iv) product throughput is faster, namely a need for time to pressurise is avoided; and\| (v) while pressurised reaction systems tend to operate in batch mode, it is much easier to configure each step, and also the overall process, as a continuous operation in an unpressurised system.\|[0046] Continuous operation is generally recognised by process engineers as preferable to batch operations because:\| (a) reaction parameters such as temperature, pH and reactant concentrations are easier to maintain at fixed optimum levels; and\| (b) residence times are shorter, thereby enabling process equipment to be smaller and cheaper and product throughput higher.\|[0047] In FIG. 2, there is provided an illustration of the details of a Carbonation process 200 as also depicted in equations 206 and 207. The Brucite (MgOH2) powder 205 is fed into a continuous reactor 201, together with a flue-gas 204. The de-carbonised flue gas 202 and Magnesium Carbonate (MgCO3) powder 203 are the reaction products of this Carbonation process 200.\|[0048] In a further embodiment of the present invention, Mg(OH)2 (Brucite) powder is provided as added to water to form an aqueous suspension which is then used at ambient temperature and pressure to scrub CO2 from a gaseous mixture of nitrogen (N2) and CO2.The scrubbing process using wet-Brucite which simultaneously removes the CO2 from the gas mixture and converts the Brucite to magnesium carbonates. Substantial removal and conversion can be achieved such that most, if not all, of the CO2 is taken out of the gas mixture and most, if not all, of the Brucite is converted.\|[0049] Following a particular example of such a further embodiment of the invention, consider the following experiment:\|A gas mixture of (nitrogen) N2 containing 4-5% CO2 (carbon dioxide, cylinder pre-mix) was bubbled continuously at a fixed flow-rate (around 2.25 litres/minute) through a fixed circulating volume (around 10 litres) of water (pre-saturated before the experiment with 5%CO-N2) containing a suspension of magnesium hydroxide powder (0.871 mol, 50.8 grams). The CO2 concentration in the exit gas was initially zero (as it was totally removed by reaction with Brucite) and was monitored as the suspended Brucite particles were consumed in the reaction to form dissolved magnesium bicarbonate. Periodic samples of the circulating liquid were taken to monitor change in pH and magnesium ion concentration. The experiment was concluded when the concentration of CO2 in the exit gas had increased to equal that of the inlet concentration, indicating that no further reaction was occurring. The experiment took approximately 12 hours to complete and was run over the course of two days with an overnight shut-down.\|[0050] A Down-flow Gas Contactor (DGC, WRK Design & Services Ltd) with a liquid volume of around 10 litres was used as the gas-liquid reactor. In this reactor, the gas-mixture at atmospheric pressure entered at the top of a bubble column, entrained in a downward circulating liquid flow. The rate of liquid recirculation in the DGC reactor (around 10 litres/min) was adjusted to maintain a stable bubble-liquid interface. The CO2-depleted gas exited from the bottom of the column after reaction and separation from the recirculating liquid phase. Gas flow rate was measured by calibrated glass tube rotammeter at a fixed 2.25 litres/minute (atmospheric pressure).\|[0051] Concentration of CO2 was measured using a calibrated inline infrared datalogger (range: 0-5 % CO2 measured to nearest 0.25 %). Temperature was ambient, in a range of 9.5-11 °C. Solution pH was in a range of pH 8.2-8.9.\|[0052] The DGC reactor provides a large and dynamic interfacial area between gas bubbles and circulating liquid. During the course of the experiment, CO2 dissolves from the gas (g) into the liquid (I) phase (or aqueous phase, aq) and reactions occur with the suspended Brucite particles (solid phase being labelled as s):\| CO2 (g) = CO2 (aq) (E1)\| CO2 (aq) + H2O(I) = H2CO3 (aq) (E2)\| H2CO3 (aq) = H+(aq) + HCO3-(aq) (E3)\| HCO3-(aq) = H+(aq) + CO32-(aq) (E4)\| Mg(OH)2(s) = Mg2+(aq) + 2OH-(aq) (E5)\| Mg(OH)2(s) + CO2(aq) = MgCO3(s) + H2O(I) (E6)\| Mg(OH)2(s) + 2CO2(aq) = Mg2+(aq) + 2HCO3-(aq) (E7)\| Mg2 +(aq) + CO32-(aq) = MgCO3(s) (E8)\| MgCO3(s) + CO2(aq) = Mg2+(aq) + 2HCO3-(aq) (E9)\|[0053] In alkaline solution, Brucite solubility is well known to be negligible while CO2 dissolves readily. In the pH range of the experiment, pH falls in the range 8.2-8.9, the predominant form of carbon in solution is the bicarbonate ion, HCO3- (aq). The dominant reactions in this situation may therefore be expected to be:\| CO2 (g) + H2O(I) = H+(aq) + HCO3-(aq) (E10)\|and\| Mg(OH)2(s) + 2H+(aq) = Mg2+(aq) + 2H2O(I) (E11)\|[0054] At higher pH, where carbonate ions dominate, the formation of solid magnesium carbonate phases would be expected and, moreover, may precipitate on the surface of the suspended Brucite particles, blocking the Brucite to further reaction with CO2.At lower pH, dissolution of CO2 would be inhibited. However, at pH 8-9, where bicarbonate ions are greatly in excess of carbonate ions, formation of solid magnesium carbonate phases should be minimal, with the result that suspended Brucite particles should fully react with CO2, ideally in a mole ration of 1:2, to form an aqueous solution of magnesium bicarbonate.\|[0055] CO2 concentrations in exit gas were data-logged continuously. Occasional measurements of (fixed) inlet CO2 concentration were taken. The resulting data is shown in the two charts: one for day 1 detailing results 1200 (Fig. 12a) and one for day 2 detailing results 1201 (Fig 12b), 5 showing CO2 concentration (%CO2) versus time.\|[0056] Analysis: The total amount of CO2 removed from the inlet gas is calculated from the measured gas flow-rate and the measured difference between inlet and outlet gas concentration: \|[0057] Uncertainty in the flow-rate measurement (rotameter) is estimated from rotameter specifications as 3 %. The CO2 meter was able only to measure to the nearest 0.5 % in a CO2 concentration range of 0-5 %. Additionally, the inlet gas CO2 concentration from the pre-mix cylinder was measured at different times in the experiment as 4 % and 5 %. Absolute uncertainty in the measured % CO2 concentration change is estimated at 0.7 % CO2.\|[0058] The total amount of CO2 removed from the inlet gas during the 12 hour course of the experiment was measured as 1.87 moles (± 0.2 moles). Within experimental error, this is the amount of CO2 expected to be removed if all 0.871 moles of the initial Brucite had reacted with CO2 to form dissolved magnesium bicarbonate according to reaction (E7) above. Within the limits of measurements errors, results show that 100 % utilisation (carbonation) of Brucite is feasible when wet-scrubbing 5 % CO2-N2 gas mixture.\|[0059] Results also show that for the first 3.5 hours of the 12 hour experimental period, removal of CO2 from the inlet 5 % CO2-N2 gas mixture was 100 %. Over the first 6 hrs (first day), CO2 removal averaged 93 % and over the full 12 hours averaged 62%. Results show unequivocally that a Brucite-water suspension can fully scrub CO2 from dilute gas mixtures.\|[0060] It may be expected that in a future industrial CO2 scrubbing system, in which the rates of water, Brucite and CO2 addition may be controlled to maintain pH within a range of around pH 8 to pH 9, and where magnesium bicarbonate is removed, continuous removal of CO2, controllable up to 100%, should be possible and/or simultaneous with up to 100% conversion of Brucite to magnesium carbonates.\|[0061] Referring to "unpressurized" mentioned in the foregoing, it is optionally feasible to vent apparatus for implementing embodiments of the present disclosure directly to ambient atmosphere, namely substantially 1 Bar pressure, thereby avoiding a need for using expensive pressure vessels. However, optionally, embodiments of the present disclosure are operated in a substantially unpressurized manner at pressures in a range of 0.5 Bar to 10.0 Bar, more optionally in a range of 0.8 Bar to 5.0 Bar, and yet more optionally in a range of 0.9 Bar to 2.0 Bar. It will be appreciated that "pressurized", in contradistinction, refers to pressures, for example, in excess of 20 Bar, in excess of 50 Bar, or even in excess of 100 Bar.\|[0062] For example, the first steps of the process in which a mined magnesium silicate mineral is converted into magnesium hydroxide can be carried out at the mine site, while, without a need for elevated temperatures or pressures for reaction, the final step in which CO2 in flue-gas reacts with aqueous magnesium hydroxide, can be carried out at a distant source of CO2 emissions, such as a power station or on board a ship. Moreover, compared with magnesium silicate or the reaction mixture, magnesium hydroxide, having a lower molar mass and being able to react more completely with CO2, has a much higher CO2 sequestration capacity, namely tonnes of CO2 stored per tonne of magnesium hydroxide that is carbonated; this means that less material needs to transported and used to sequester the same mass of CO2 and, therefore, less energy and cost is expended in transport and handling tasks. In a non-inventive alternative embodiment, in which magnesium hydroxide powder is replaced with magnesium silicate powder in water slurry, it is surprisingly found, pursuant to the present disclosure, that it is also possible to achieve substantial direct aqueous-phase carbonation of Serpentine and Olivine powders, and substantial scrubbing of CO2 from ambient pressure flue gas. The prior art teaches that substantial and direct carbonation of Serpentine or Olivine powders is only possible under energy-intensive and costly conditions of elevated temperature or pressure, or with intense pre-processing, or with chemical additives. Pursuant to the present disclosure, it is found that high efficiency and low-cost non-inventive direct carbonation of Serpentine and Olivine can be achieved at ambient pressures and temperatures with only water or seawater and CO2 as additives in a simple carbonation reactor system. The CO2 can be pure or dilute, as in flue-gas or even in air, and at any partial pressure or temperature. In an embodiment of the present disclosure, there is injected simulated flue gas, namely a mixture of CO2 and N2, into a circulating slurry of the mineral powder in water and also in seawater. Many alternative gas-liquid mixing arrangements are possible, such as spraying of droplets solution of slurry into the gas. Similarly, many non-inventive alternative arrangements for solids-liquid mixing are possible, such as a fixed or stirred bed, or column of mineral particles through which water or brine is circulated to dissolve the mineral. By controlling a rate at which CO2 and/or mineral and/or water and/or energy are added or removed to/from the system, it was surprisingly found that conditions can be maintained in which the magnesium silicate mineral continuously dissolves and the CO2 is continuously scrubbed from the gas. Measurements of water containing Serpentine powder demonstrate an alkaline pH above pH8, and even above pH9. Serpentine and Olivine and other related magnesium silicate minerals such as chrysotile, lizardite, antigorite, and forsterite are composed of alternating crystal layers of magnesium oxide/hydroxide and silica. It is believed that the mechanism by which the magnesium silicate mineral dissolution and carbonation is possible under such mild conditions is that a suitable pH in the range of pH 8 to pH 9 is maintained by the addition of CO2, such that successive crystal layers of magnesium hydroxide dissolve directly into solution to form a solution of magnesium bicarbonate. In this pH range, carbonate ion concentration in solution is orders or magnitude lower than bicarbonate ion concentration and the formation of passivating solid magnesium carbonate phases on the surface of magnesium silicate particles is therefore avoided. Dissolution of the magnesium oxide layers is likely to destabilise the successive silica layers in the magnesium silicate crystal, so that the silica dissolves or precipitates as a solid, possibly accelerated by surface attrition due to stirring or solution circulation. The advantages pertaining to this surprising beneficial result of being able to carbonate magnesium silicate mineral powders according to a non-inventive process, namely without any pre-processing other than mining and crushing operations, directly under ambient conditions with just water and dilute CO2 are several, namely:\| (i) magnesium silicate mineral powders are much cheaper as feedstocks for carbonation than magnesium hydroxide, or thermally or chemically activated magnesium silicate mineral powers;\| (ii) carbonation can potentially be carried out directly at a huge scale at the site of the magnesium silicate mineral deposit using the CO2 available in air, or CO2 piped to the site, and with recirculation of water no additional water supply is needed;\| (iii) recovery and separation of pure CO2 gas and pure solid magnesium carbonate from the bicarbonate solution by conventional ageing, thermal or pressure-swing processes can provide compatibility with other CO2 transport, storage or utilisation options;\| (iv) separation of pure solid magnesium carbonate from bicarbonate solution provides a saleable chemical and industrial feedstock for other processes;\| (v) separation of silica solids from the dissolution/disintegration of the magnesium silicate mineral provides a further saleable industrial feedstock; and\| (vi) Nickel and Iron and other minor elemental constituents typically present in magnesium silicate minerals and wastes may be released in the process and can potentially be economically recovered from solution or by purification of the solid products.\|[0063] The efficiency of this entire process as illustrated in FIG. 1 and FIG.2 has been analysed through various scalability experiments, wherein it has been found that, for the Magnesium-mineral Silicates, the alkaline treatment is attractive as the associated Carbonation reaction is chemically favourable at a higher pH resulting in a higher reaction rate:\| Mg2SiO4 + 2NaOH +H2O => 2Mg(OH)2 (↓) +Na2SiO3 (aqueous) (8)\| Mg(OH)2 + CO2 => MgCO3 (↓) + H2O (9)\|[0064] In one of the embodiments, it is feasible to convert Dunite, an ultramafic rock rich in Magnesium-bearing minerals, into Magnesium Hydroxide (Mg(OH)2) by using highly concentrated Sodium Hydroxide (NaOH) aqueous solutions. The effect of the reaction time and the Sodium Hydroxide (NaOH) solution concentration on the process were studied to determine optimal conditions for achieving higher rate of conversion of Magnesium-mineral Silicates into Magnesium Hydroxide (Mg(OH)2). The product phases were identified by XRD and TG analysis. Careful quantification of Forsterite and Brucite both in raw materials and products were performed using Rietveld Refinement QPA and TG. The experimental results have been illustrated in the FIG. 3a and 3b FIG. 4a and 4b, FIG. 5, FIG. 6, Fig. 7a and 7b, FIG. 8, FIG. 9, FIG. 10, FIG. 11a and 11b; these results are indicated by 300, 301, 400, 401, 500, 600,700, 701, 800, 900, 1000, 1100, 1101 respectively. The experimental results of these drawings have been briefly elucidated in the foregoing.\|[0065] The tests conducted have shown that Magnesium-mineral Silicates constituting Dunite can be almost completely substituted with Brucite in highly concentrated solutions of Sodium Hydroxide (NaOH) and heated to a temperature of substantially 180 °C. According to the experimental results, increasing the Sodium Hydroxide (NaOH) concentration and the time of reaction are both factors that positively affect the conversion of Magnesium-Silicates into Magnesium Hydroxide. A greater amount of Magnesium Hydroxide (Mg(OH)2) was produced by using either a solution of Sodium Hydroxide (NaOH) having a molar concentration of 50 mol/kg for a temporal duration of 6 hours (73 wt%), or by using a solution of Sodium Hydroxide (NaOH) having a molar concentration of 40 mol/kg for a temporal duration of 18 and 24 hours (79 - 80 wt%). The TGA analyses results were found to be in accordance with the qualitative XRD results and with the Rietveld Refinement Quantitative Phase Analysis.\|[0066] During our exploration of optimal experimental conditions for different embodiments of the Olivine-NaOH reaction, we have discovered that it is possible to achieve substantial conversion of Olivine to Brucite in open vessels at ambient atmospheric pressure while heating to temperatures in the range 130-220 °C. At these elevated temperatures the vapour pressure of water significantly exceeds the reaction pressure. This discovery provides a significant advantage over the processes described by prior art systems in that the reaction can be conducted at much lower pressures (and even at ambient atmospheric pressure) using standard low-cost industrial reactors that typically are designed to withstand operating pressures up to 10 Bar.\|[0067] In accordance with another embodiment of the present invention, compacted Dunite powder can be heated in a sealed vessel at a temperature around 180°C, preferably for around six hours, to produce a product comprising Brucite.\|[0068] In accordance with another embodiment of the present invention, the Olivine and/or Serpentine is a Magnesium mineral which are suitable feedstock materials due to their high content of Magnesium (Mg) and wide abundance and large concentration in mineralogical sites.\|[0069] From the above description and claimed process, it will be appreciated that there is provided an improved process of alkali digestion for mineral Carbonation. The process can find utility in sequestration of Carbon Dioxide (CO2), extraction of valuable minerals, and other processes, known to the person skilled in the art, requiring the digestion of minerals for their Carbonation.\|[0070] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) comprises:\| reacting an alkaline earth silicate-based material with an alkali metal compound to form a mixture comprising a hydroxide of the alkaline earth, wherein the alkali metal is selected from sodium and/or potassium, and wherein the alkaline earth is selected from magnesium and/or calcium;\| reacting the mixture at a temperature in the range 140-220 °C and at a pressure of less than 10 Bar;\| separating the hydroxide of the alkaline earth from the mixture; and\| combining the hydroxide of the alkaline earth with a source of Carbon dioxide (CO2) producing a Carbonate or Bicarbonate or the alkaline earth. This gives a very beneficial production and sequestration of the hydroxide of the alkaline earth.\|[0071] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above further includes reacting the mixture in (b) at a pressure of less than the vapour pressure of pure water at the temperature of reaction.\|[0072] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above further includes using the mixture with a stoichiometric ratio between the Si in the alkaline earth silicate-based material and the alkali metal in the alkaline compound in a range of 1:1 to 1:2.\|[0073] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes using the mixture in a form of an aqueous solution with the molality of >30 molar of alkaline compound per litre water (H2O).\|[0074] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes reacting the mixture at ambient atmospheric pressure.\|[0075] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes executing the reaction at a temperature of ca 180 °C.\|[0076] Optionally, a non-inventive method of sequestration Carbon Dioxide (CO2) as outlined above includes using flue gases with less than 50vol% Carbon Dioxide (CO2) as part of a gas mixture for carbonation.\|[0077] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes carrying out reactions in an unpressurised continuous mode to achieve substantially complete carbonation of the Magnesium Hydroxide or Magnesium silicate.\|[0078] Optionally, a non-inventive system for sequestrating Carbon Dioxide (CO2), wherein the system includes a first reaction chamber which is operable to receive a Silicate-based material and an alkaline compound, and a blending apparatus for blending contents of the first reaction chamber to produce a mixture therein.\|[0079] Optionally, the non-inventive system for sequestrating Carbon Dioxide (CO2) as described above is operable to execute the method outlined above method of sequestrating Carbon Dioxide (CO2).\|[0080] Modifications to embodiments of the invention described in the foregoing are possible without departing from the scope of the invention as defined by the accompanying claims. For example the compound in the reaction may be selected from any one or combination of Hydroxide, Carbonate, and/or Bicarbonate as would be suitable to the person skilled in the art. Expressions such as "including", "comprising", "incorporating", "consisting of", "have", "is used to describe and claim the present invention are intended to be construed in a non-exclusive manner, namely allowing for items, components or elements not explicitly described also to be present. Reference to the singular is also to be construed to relate to the plural. Numerals included within parentheses in the accompanying claims are intended to assist understanding of the claims and should not be construed in any way to limit subject matter claimed by these claims.	(EP3129125)\|TECHNICAL FIELD\|[0001] The present disclosure relates to methods of producing activated mineral silicate for use in sequestrating Carbon Dioxide, for example from flue-gas, by utilizing a process which involves digestion of metal mineral Silicates. Moreover, the present disclosure also relates to systems for executing aforesaid methods.\|BACKGROUND\|[0002] Increasing concentrations of Carbon Dioxide (CO2) in the Earth's atmosphere have recently caused concerns, as the present concentrations are substantial at 400 p.p.m. and increasing at a rate of 4 p.p.m. per annum. A major factor contributing to such increase is the anthropogenic oxidation of carbonaceous fossil fuels, for example coal, oil and gas. The World presently consumes circa 100 million barrels of oil per day.\|[0003] There have been recent initiatives to employ more renewable energy systems, for example wind turbines and tidal power generating systems, as well as sequestration of Carbon Dioxide (CO2) from flue-gases emitted from coal burning electricity generating facilities. Thus, primary initiatives involve utilizing energy efficient technologies, increasing reliance on renewable sources, and developing technologies for long term storage of Carbon Dioxide (CO2) emissions. The latter technology field is known as Carbon Dioxide (CO2) sequestration.\|[0004] There have been significant developments in Carbon Dioxide (CO2) sequestration in recent years, and Carbon Dioxide sequestration technologies have aroused considerable interest among governments, industries and scientific communities. Earlier methods of Carbon Dioxide (CO2) sequestration suffered from various drawbacks such as risk of water contamination, and a lack of suitable storage spaces for receiving sequestrated Carbon Dioxide (CO2); these drawbacks are familiar to a person skilled in the art.\|[0005] There has been considerable interest in mineral Carbonation technologies to address aforementioned problems associated with known Carbon Dioxide (CO2) sequestration. The Masters thesis by Mabell Delgado Torróntegui at ETH in Switzerland, "Assessing the Mineral carbonation science and technology" (2010), provides an overview of contemporary research in this field of Carbon Dioxide (CO2) sequestration technology. A key principle of mineral Carbonation is also known as "mineral sequestration technology", wherein sequestration of Carbon Dioxide (CO2) is achieved by capturing Carbon Dioxide (CO2) in a form of stable mineral Carbonates. Such sequestration employs a process which is an exothermic reaction of a metal Oxide and Carbon Dioxide (CO2) to form stable Carbonate materials as provided in a reaction formula (1):\| MO + CO2 => MCO3 + Heat (1)\|wherein M is a metal, preferably an alkaline earth metal such as Calcium or Magnesium.\|[0006] Most suitable and naturally abundant sources of these metal Oxides are Magnesium or Calcium Silicate minerals such as Olivine, wollastonite, and Serpentine. The Carbonation reactions of these minerals are as follows:\| Olivine:\| Mg2SiO4 + 2CO2 => 2MgCO3 + SiO2 + 89 kJ mol-1CO2 (2)\| Serpentine:\| Mg3Si2O3(OH)4 + 3CO2 => 3MgCO3 + 2SiO2 + 2H2O + 64 kJ mol-1CO2\| Wollastonite:\| CaSiO3 + CO2 => CaCO3 + SiO2 + 90 kJ mol-1CO2 (4)\|[0007] Although the above reactions (2) to (4) are thermodynamically favourable, the reactions in nature have, however, relatively slow reaction rates in a geologic time scale, and are unsuitable for industrial processes. Efforts have been made to try to accelerate these reactions. However, the efforts suffer from various limitations, such as energy wastage and a high cost of mining and transporting large amounts of rock, as well as industrial and environmental inefficiencies. Moreover, the mineral Silicates are not easily obtainable in suitable quantities and formats for allowing satisfactory mineral Carbonation to be achieved.\|[0008] In a published US patent no. US7604787B2 (MAROTO-VALER), "Process for sequestering Carbon Dioxide and Sulphur Dioxide", there is described a method of reacting a Silicate-based material with an acid to form a suspension, which is then combined with Carbon Dioxide to produce a metal salt, silica and regenerating acid in solution. This method has drawbacks of being environmentally harsh and inefficient. Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for removal and Capture of Carbon Dioxide from Flue Gases".\|[0009] Although, the prior art disclosures have been able to address some of the problems of mineral Carbonation through their indirect sequestration processes, there are several remaining problems which have not yet been resolved. Such remaining problems pertain to industrial scalability, environmental efficiency, and cost.\|[0010] Lately, research effort has focused upon Carbon Dioxide (CO2) sequestration by 'direct' Carbonation of Olivine or Serpentine. In these recent methods, Carbon Dioxide (CO2) is sequestered without acid pretreatment of Silicate feedstock. An Olivine reaction is:\| Mg2SiO4 + 2CO2 → 2MgCO3 + SiO2 (5)\|[0011] Moreover, for Serpentine, a corresponding reaction is:\| Mg3Si2O5(OH)4 + 3CO2 → 3MgCO3 + 2SiO2 + 2H2O (6)\|[0012] Experiments to determine the kinetics of these reactions (5) and (6) have shown that such reactions also suffer from poor energy efficiency and a high cost when up-scaled to an industrial plant. In order to accelerate the reactions (5) and (6), high temperatures in a range of 600°C to 650 °C are required. In a fuel-fired industrial power plant, attainment of such high temperatures would translate to a requirement of approximately 200 kW-h of electricity per tonne of Serpentine feedstock. Moreover, with a fossil fuel containing 1 tonne of Carbon, nearly 3.7 tonnes of Carbon Dioxide (CO2) is produced. Each tonne of Carbon Dioxide (CO2) consumes more than 2 tonnes of Serpentine during Carbonation. Combined with a pre-capture step to separate and pressurise CO2 from flue gas, the power required for Serpentine dehydroxylation Is around 20-30% of total power output from such fuel-fired industrial power plant. All these considerations lead to a huge energy penalty threatening the economic feasibility of this sequestration process.\|[0013] In a published US patent no. US8114374B2 (BLENCOE), "Carbonation of metal Silicates for long-term CO2 sequestration", there is described a method (hereinafter "Blencoe's method") of reacting a Silicate with an alkali metal hydroxide in an aqueous solution. The reaction with Carbon Dioxide (CO2) is then used to carbonate the metal formerly contained in the metal Silicate. This method has drawbacks of inefficiencies and poor overall Carbon capture properties. Blencoe's method comprises three steps:\| (1) reacting a metal silicate with a caustic alkali-metal hydroxide to produce a hydroxide of the metal formerly contained in the silicate;\| (2) reacting carbon dioxide with at least one of a caustic alkali-metal hydroxide and an alkali-metal silicate to produce at least one of an alkali-metal carbonate and an alkali-metal bicarbonate; and\| (3) reacting the metal hydroxide product of step (a) with at least one of the alkali-metal carbonate and the alkali-metal bicarbonate produced in step (b) to produce a carbonate of the metal formerly contained in the metal silicate of step (a).\|[0014] In Blencoe's first step (1), the alkali-metal hydroxide is in aqueous solution which limits the maximum reaction temperature to the vapour pressure of the aqueous solution at the pressure under which the reaction is carried out. A low reaction temperature limits the reaction rate at atmospheric pressure, while use of a pressurised vessel increases process costs. Alkali-metal hydroxides, such as NaOH and KOH, used in steps (1) and (2) are energy intensive and expensive chemicals to manufacture. In Blencoe's second step (1), alkali-metal hydroxide, additional to that used in step (1), is used to react with Carbon Dioxide. In Blencoe's second and third steps (2) and (3), an elevated pressure is required, namely having implied costs of a pressure vessel, in the range between the vapour pressure of water at the reaction temperature and Bar. It is doubtful that the overall process described is able to sequester more Carbon Dioxide as a metal carbonate than is generated as a consequence of manufacture of the alkali-metal hydroxides consumed in the process, or that the process is any cheaper to operate than Carbon Dioxide sequestration processes described in the prior art.\|[0015] Therefore, there is an urgent need to develop a process which is energy efficient, has a high throughput and is more cost effective than the prior art so that it can be used industrially.\|[0016] From the foregoing, it will be appreciated that the known methods of processing and the systems for mineral carbonation and Carbon Dioxide (CO2) sequestration, are neither optimal in their manner of operation nor adaptable to broader applications in a cost effective manner.\|SUMMARY\|[0017] The present invention seeks to provide an improved method of activation of magnesium silicate minerals by conversion to magnesium hydroxide.\|[0018] This present embodiment of the invention allows for a method of large scale industrial use and continuous carbonation without advanced pressure chambers or equipment.\|[0019] The present invention provides a method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, wherein the method comprises:\| a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from a group comprising alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture;\| b. heating the dry solid-solid mixture to a temperature below 300°C in an unpressurised vessel for less than 4 hours to form a solid glass product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate; and\| c. dissolution of the solid glass product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products.\|[0020] Optionally, the method includes the liquid slurry of step c being separated into solid and aqueous solution phase products.\|[0021] Optionally, the method includes reacting any of the aqueous phases at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|[0022] Optionally, the method includes mixing the solid phase product with water and reacted at atmospheric pressure with a gas comprising 0.04%-100% CO2.\|[0023] Optionally, the method includes air or flue gas as the gas in the reaction. This allows for a very simple and cost-effective solution utilizing what is available at the site of operation.\|[0024] Optionally, the method includes using a hydroxide or a carbonate of sodium or a potassium as the alkali metal compound in the reaction.\|[0025] Optionally, the method includes a serpentine or an olivine rock as the magnesium silicate mineral in the reaction. Further, optionally, the method includes heating the unpressurised vessel in step (b) to a temperature in the range 140 °C - 220 °C.\|[0026] Optionally, the method includes continuously adding the magnesium silicate mineral and alkali metal compound of step (a) together allowing continuous reacting thereof under the conditions of step (b) and further continuously removing the product of step (b).\|[0027] Optionally, the method includes the molar ratio of substantially 2 moles of alkali metal per mole of silicon in the mixture.\|[0028] Additional aspects, advantages, features and objects of the present invention would be made apparent from the drawings and the detailed description of the illustrative embodiments construed in conjunction with the appended claims that follow. It will be appreciated that features of the present invention are susceptible to being combined in various combinations from different embodiments without departing from the scope of the present invention as defined by the appended claims.\|DESCRIPTION OF DRAWINGS:\|[0029] The summary above, as well as the following detailed description of illustrative embodiments, is better understood when read in conjunction with the appended drawings. For the purpose of illustrating the present invention, exemplary constructions of the disclosure are shown in the drawings. However, the present invention is not limited to specific methods and apparatus disclosed herein. Moreover, those in the art will understand that the drawings are not to scale. Wherever possible, like elements have been indicated by identical numbers.\| FIG. 1 is an illustration of a flow chart of a digestion Step 1 involving alkaline digestion of Serpentine or Olivine to convert them to Brucite and Silica;\| FIG. 2 is an illustration of a flow chart of a Carbonation step 2 involving direct Carbonation of Brucite, namely Magnesium Hydroxide, with flue-gas to form Magnesium Carbonate;\| FIG.3a and 3b are illustrations of XRD patterns of selected samples, wherein solid products from dissolution of Dunite, namely a form of Olivine, using Sodium Hydroxide (NaOH) solution of concentration in a range of 15 to 40 mol/kg (left), and using Sodium Hydroxide (NaOH) solution of concentration 50 mol/kg (right) solutions. In the illustrations, following abbreviations are employed: Fo = Forsterite, Brc = Brucite, Clc = Clinochlore, En = Enstatite, Srp = Serpentine, Tlc = Talc, Spl = Spinel;\| FIG. 4a and 4b are illustrations of TG (4a) and DTG (4b) curves of selected samples: solid products from dissolution of Dunite at a temperature of 180°C for 15 for 6 hours with different concentrations of Sodium Hydroxide (NaOH) solution;\| FIG. 5 is a graph wherein there are shown Mg(OH)2 concentrations in solid products based on TG results: Dunite dissolved at a temperature of 180°C with different concentrations of Sodium Hydroxide (NaOH) solution, namely measured as moles of NaOH per kg of water. From the graph, it will be appreciated that the proportion of Dunite, namely magnesium silicate, converted to Brucite, namely magnesium hydroxide, increases approximately linearly with increase in NaOH concentration; extrapolation of this graph indicates that the proportion of Brucite in the solid product should approach 100% above a NaOH concentration >70mol/kg, namely equivalent to a NaOH: H2O ratio >1.26;\| FIG. 6 is an illustration of XRD patterns of solid products from dissolution of Dunite at 180 °C with Sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg solution, for different temporal durations;\| FIG. 7a and 7b are illustrations of TG (7a) and DTG (7b) curves of solid products from dissolution of Dunite at a temperature of 180° C with sodium Hydroxide (NaOH) solution having a molar concentration of 40 mol/kg for different temporal durations;\| FIG. 8 is a graph in which there is shown Magnesium Hydroxide Mg(OH)2 concentration in solid products based on TG results: Dunite dissolved at a temperature of 180 °C with a molar concentration of Sodium Hydroxide (NaOH) solution being 40 mol/kg for different durations;\| FIG. 9 is an illustration showing Rietveld Refinement QPA of raw Dunite, wherein: data points profile = experimental pattern; continue profile = calculated model (above); difference plot (below);\| FIG. 10 is an illustration showing Rietveld Refinement QPA of dissolved Dunite spiked with 10 wt% Silicon, wherein: data points profile = experimental pattern; continue profile = calculated model; and\| FIG. 11a and 11b are illustrations showing Brucite quantification with Rietveld Refinement and TGA (FIG. 11a), wherein Forsterite and Brucite concentrations were obtained via Rietveld Refinement QPA of selected samples (FIG. 11b).\| FIG. 12a and 12b depict experimental data concerning the removal of CO2 by means of Brucite powder in aqueous suspension, specifically the resulting CO2 level for a monitored exit gas after processing.\|[0030] In the accompanying drawings, an underlined number is employed to represent an item over which the underlined number is positioned or an item to which the underlined number is adjacent. A non-underlined number relates to an item identified by a line linking the non-underlined number to the item. When a number is non-underlined and accompanied by an associated arrow, the non-underlined number is used to identify a general item at which the arrow is pointing.\|DETAILED DESCRIPTION OF EMBODIMENTS\|[0031] The following detailed description illustrates embodiments of the present disclosure and ways in which they can be implemented.\|[0032] In FIG. 1, there is shown a digestion process 100, wherein there occurs alkaline digestion of a Silicate-based material, a naturally occurring feedstock containing magnesium or calcium silicate, such as Serpentine, Olivine, Dunite, and/or Wollastonite 101. The process 100 results in reaction products being generated, namely a conversion to Brucite and Silica in a case of Olivine 101 being a feed mineral employed. In the reaction, Olivine 101 is fed into a stirred reactor 102 together with an alkali 103 and heat is provided from a heat source 104. The alkali is beneficially selected from a mineral Hydroxide. Among the many metal Hydroxides that can find utility in this reaction, a preferable alkali used is Sodium Hydroxide (NaOH) .\|[0033] The reaction mixture of the digestion process 100 comprises a stoichiometric ratio between the soluble silicate based material and the solid hydroxide of the alkaline earth compound of about 1:2. This stoichiometric ratio aims to minimise the input of the alkaline compound, such as Sodium Hydroxide (NAOH), into the initial reaction mixture. This limits the regeneration of Sodium Hydroxide (NaOH) from carbonates at the end of the reaction, which is costly and time consuming. The reaction mixture is a dry mixture.\|[0034] According to a further embodiment, the reaction mixture is a solid-state dry mixture of a powder of the alkaline-earth silicate and the alkali-metal compound, in the stoichiometric ratio of one mole of silicon, namely in the silicate, per two moles of alkali-metal. Solid alkali-metal compounds, such as NaOH, KOH and Na2CO3, have high melting points, namely 318°C, 406°C and 851 °C, respectively. Using an aqueous system, such as taught by Blencoe, would therefore be expected to be essential to achieving mixing and reaction at temperatures below 300 °C. Surprisingly, in experiments using NaOH and Serpentine, namely magnesium silicate, it is found that a dry solid state mixture of the two rapidly melted, mixed and reacted to form magnesium hydroxide in an unpressurised vessel at temperatures as low as 180°C, namely well below the melting temperature of NaOH, namely 318°C, or of Serpentine, namely >1700 °C. Unlike Olivine, Serpentine has a crystal structure that contains chemically bound hydroxide groups, and it is believed that these groups may facilitate the dry stoichiometric reaction to form magnesium hydroxide.\|[0035] Dunite can also be used to yield Mg(OH)2 via solid state reaction, with a preferable ratio of Dunite to NaOH in a mole ratio of 1:2, at a temperature around 180 °C. Experiments conducted with a range of Dunite: NaOH mole ratios of 1:0.5, 1:1, 1:.5 and 1:2, where the powder has been formed into pellets by compaction with a hand press (3 tonnes for 1 minute for compression), returned results indicating a linear increase of Mg(OH)2 production with increase of NaOH, to a maximum weight percentage of Mg(OH)2 in the reaction products of around 46.7%. Reducing the amount of NaOH significantly lowered the extraction efficiency of the process.\|[0036] In contrast, results of non-inventive experiments, as provided in FIGs. 3a, 3b, 5, with aqueous NaOH and Olivine show that minimum reaction conditions of a temperature of 180°C and a NaOH concentration of 40mol/kg are substantially required to form magnesium hydroxide; this system requires a pressure vessel to reach a required reaction temperature.\|[0037] For the case of Dunite samples, comparison of the results cited above with alkaline digestion of Dunite with 50mol/kg NaOH aqueous system at 180°C under a similar time period, show that the yield of Mg(OH)2 via solid state reaction (55% to 62%) was on a par with that produced using the aqueous system (between 58% and 66%). The alkaline digestion with 50mol/kg NaOH required significantly more NaOH per 1 gram of Dunite processed such that the solid state reaction effected a 97% to 99% reduction of NaOH consumption. Additional experimental results comprising Dunite as a sample component are detailed later.\|[0038] Generally stated, it has been demonstrated that it is possible to extract Mg(OH)2 from magnesium containing silicate minerals via solid state reaction with NaOH and that the consumption of the alkaline reactant can be reduced, achieving significant yield of reaction. An additional advantage is the reduction of water consumption which would be needed for an aqueous process.\|[0039] Moreover, results have also shown, namely in FIG. 5, that without water, the NaOH concentration (mol/kg) effectively approaches infinity and might therefore be expected to approach 100% conversion of magnesium silicate to magnesium hydroxide. Compared to the aqueous reaction system, as exemplified by Blencoe, clear benefits of the non-aqueous dry-mixture and stoichiometric system using Serpentine are that:\| (i) no pressure vessel is required;\| (ii) melting and mixing surprisingly take place at 180 °C, to enable a rapid reaction at a rate similar to an aqueous system;\| (iii) a highest possible concentration and activity of NaOH is enabled, leading to a faster and more complete reaction than possible in an aqueous system at a similar temperature;\| (iv) the NaOH is totally consumed in a reaction with silicate to form solid sodium silicate, so that no subsequent process for recovery of excess NaOH from the reaction products is required;\| (v) Serpentine provides any water required for the stoichiometric conversion to magnesium hydroxide from its structural hydroxide groups, so that no free water needs to be added to the reaction system;\| (vi) the products of reaction, containing no excess NaOH, are a solidified glass which is substantially less caustic than in the aqueous process and are therefore much safer to handle;\| (vii) sodium silicate is readily separated from the products of reaction by dissolution and filtration, and is available without contamination by NaOH; and\| (viii) the process can be more readily and cheaply carried out at remote Serpentine or Olivine mine sites where water may not be available.\|[0040] Further, in the prior art of Blencoe it is described how the initial step (a) can be conducted at a pressure slightly below the vapour pressure of pure water for the temperature of that step. Blencoe does not claim a preferred temperature or pressure or aqueous solution composition for that initial step (a), but in a table of experimental results shows that all reactions in which serpentine or olivine are converted to a major phase of brucite are done in aqueous solution in a pressure vessel at a temperature of 200 °C and pressure <15atm. One experiment conducted at a temperature of 22 °C and 1atm pressure for 72hrs results in conversion to a minor phase of brucite; subsequent additional reaction at 200 °C and < 15bar then converts substantially to brucite with a minor residual phase of serpentine. Notwithstanding Blencoe's assertion of the technological and commercial advantage of avoiding pressure-intensifying equipment, at the effective reaction temperature of 200 °C for Blencoe's step (a), the vapour pressure of pure water is just above bar indicating that a pressure vessel must be used in this step. The current invention allows for the method and system to operate without expensive and complicated equipment used in Blencoe to operate at higher than atmospheric pressure.\|[0041] In the example of magnesium carbonates being produced according to the described method, a wide range of compounds including soluble magnesium bicarbonate Mg(HCO3)2 is produced in solution, but generates no separate water in the carbonation reaction:\| 2CO2+ Mg(OH)2 = Mg.(HCO3)2 (7)\|[0042] The preferred alkali 103 for this digestion process is beneficially Sodium Hydroxide or Potassium Hydroxide. It is also possible to use Sodium Carbonate, Sodium Bicarbonate, Potassium Carbonate and Potassium Bicarbonate as the alkali for the digestion process.\|[0043] The heat source 104 is employed to raise a temperature of the digestion process, whilst stirring of the mixture is implemented, to a temperature of less than 250 °C, and for a temporal period of less than 6 hours. A preferred range of temperature is from 140 °C to 220 °C. The reaction can be best performed with the temperature being less than 200 °C, and most preferentially at around 180 °C, throughout the process, as shown in the results FIG. 4 to FIG. 8. The digestion vessels used are most suitably Teflon (PTEE) to withstand hot-conc-NaOH with the maximum operating temperature usually specified at 220 °C. Experiments with Magnesium silicate mineral feedstocks have been showing excellent results for this process.\|[0044] This digestion process is preferably carried out at a pressure of less than Bar, wherein 1 Bar corresponds to nominal atmospheric pressure at sea-level. The reaction can be more preferably carried out at a pressure less than 10 Bar. The reaction can be furthermore preferably be carried out at pressure conditions lower than the vapour pressure of pure water at the temperature of reaction. The benefit of not having to use high pressure vessels to carry out hydrothermal reactions saves cost and also improves the applications of the technology in industrial applications at very high volumes and large scale installations.\|[0045] The process, after digestion of Olivine, is shown in equation 112. Here, the Brucite (MgOH2) 107, solid phase, is separated from a Silicate solution 108. Thereafter, the Silica precipitation process is carried out as depicted in the equations 113 and 112. The process, namely acid precipitation, can be carried out by adding either Carbon Dioxide (CO2) or acid 110. Excess alkali 111 is recovered and fed back to a chamber of the reactor 102. Performing the digestion process at ambient atmospheric pressure conditions avoids a need to employ equipment to increase pressure, for example an autoclave, and allows large scale, continuous sequestration of industrial Carbon Dioxide (CO2) emissions to be achieved. Avoiding the requirement for any pressurised containment of the reaction steps, provides several benefits:\| (i) much cheaper and simpler reaction vessels can be used;\| (ii) it is easier and cheaper to incorporate mixing, stirring and/or particle attrition to enhance reaction rates within an unpressurised reaction vessel;\| (iii) energy usage, namely energy wasted in pressurisation/ depressurisation, is lower;\| (iv) product throughput is faster, namely a need for time to pressurise is avoided; and\| (v) while pressurised reaction systems tend to operate in batch mode, it is much easier to configure each step, and also the overall process, as a continuous operation in an unpressurised system.\|[0046] Continuous operation is generally recognised by process engineers as preferable to batch operations because:\| (a) reaction parameters such as temperature, pH and reactant concentrations are easier to maintain at fixed optimum levels; and\| (b) residence times are shorter, thereby enabling process equipment to be smaller and cheaper and product throughput higher.\|[0047] In FIG. 2, there is provided an illustration of the details of a Carbonation process 200 as also depicted in equations 206 and 207. The Brucite (MgOH2) powder 205 is fed into a continuous reactor 201, together with a flue-gas 204. The de-carbonised flue gas 202 and Magnesium Carbonate (MgCO3) powder 203 are the reaction products of this Carbonation process 200.\|[0048] In a further embodiment of the present invention, Mg(OH)2 (Brucite) powder is provided as added to water to form an aqueous suspension which is then used at ambient temperature and pressure to scrub CO2 from a gaseous mixture of nitrogen (N2) and CO2.The scrubbing process using wet-Brucite which simultaneously removes the CO2 from the gas mixture and converts the Brucite to magnesium carbonates. Substantial removal and conversion can be achieved such that most, if not all, of the CO2 is taken out of the gas mixture and most, if not all, of the Brucite is converted.\|[0049] Following a particular example of such a further embodiment of the invention, consider the following experiment:\|A gas mixture of (nitrogen) N2 containing 4-5% CO2 (carbon dioxide, cylinder pre-mix) was bubbled continuously at a fixed flow-rate (around 2.25 litres/minute) through a fixed circulating volume (around 10 litres) of water (pre-saturated before the experiment with 5%CO-N2) containing a suspension of magnesium hydroxide powder (0.871 mol, 50.8 grams). The CO2 concentration in the exit gas was initially zero (as it was totally removed by reaction with Brucite) and was monitored as the suspended Brucite particles were consumed in the reaction to form dissolved magnesium bicarbonate. Periodic samples of the circulating liquid were taken to monitor change in pH and magnesium ion concentration. The experiment was concluded when the concentration of CO2 in the exit gas had increased to equal that of the inlet concentration, indicating that no further reaction was occurring. The experiment took approximately 12 hours to complete and was run over the course of two days with an overnight shut-down.\|[0050] A Down-flow Gas Contactor (DGC, WRK Design & Services Ltd) with a liquid volume of around 10 litres was used as the gas-liquid reactor. In this reactor, the gas-mixture at atmospheric pressure entered at the top of a bubble column, entrained in a downward circulating liquid flow. The rate of liquid recirculation in the DGC reactor (around 10 litres/min) was adjusted to maintain a stable bubble-liquid interface. The CO2-depleted gas exited from the bottom of the column after reaction and separation from the recirculating liquid phase. Gas flow rate was measured by calibrated glass tube rotammeter at a fixed 2.25 litres/minute (atmospheric pressure).\|[0051] Concentration of CO2 was measured using a calibrated inline infrared datalogger (range: 0-5 % CO2 measured to nearest 0.25 %). Temperature was ambient, in a range of 9.5-11 °C. Solution pH was in a range of pH 8.2-8.9.\|[0052] The DGC reactor provides a large and dynamic interfacial area between gas bubbles and circulating liquid. During the course of the experiment, CO2 dissolves from the gas (g) into the liquid (I) phase (or aqueous phase, aq) and reactions occur with the suspended Brucite particles (solid phase being labelled as s):\| CO2 (g) = CO2 (aq) (E1)\| CO2 (aq) + H2O(I) = H2CO3 (aq) (E2)\| H2CO3 (aq) = H+(aq) + HCO3-(aq) (E3)\| HCO3-(aq) = H+(aq) + CO32-(aq) (E4)\| Mg(OH)2(s) = Mg2+(aq) + 2OH-(aq) (E5)\| Mg(OH)2(s) + CO2(aq) = MgCO3(s) + H2O(I) (E6)\| Mg(OH)2(s) + 2CO2(aq) = Mg2+(aq) + 2HCO3-(aq) (E7)\| Mg2 +(aq) + CO32-(aq) = MgCO3(s) (E8)\| MgCO3(s) + CO2(aq) = Mg2+(aq) + 2HCO3-(aq) (E9)\|[0053] In alkaline solution, Brucite solubility is well known to be negligible while CO2 dissolves readily. In the pH range of the experiment, pH falls in the range 8.2-8.9, the predominant form of carbon in solution is the bicarbonate ion, HCO3- (aq). The dominant reactions in this situation may therefore be expected to be:\| CO2 (g) + H2O(I) = H+(aq) + HCO3-(aq) (E10)\|and\| Mg(OH)2(s) + 2H+(aq) = Mg2+(aq) + 2H2O(I) (E11)\|[0054] At higher pH, where carbonate ions dominate, the formation of solid magnesium carbonate phases would be expected and, moreover, may precipitate on the surface of the suspended Brucite particles, blocking the Brucite to further reaction with CO2.At lower pH, dissolution of CO2 would be inhibited. However, at pH 8-9, where bicarbonate ions are greatly in excess of carbonate ions, formation of solid magnesium carbonate phases should be minimal, with the result that suspended Brucite particles should fully react with CO2, ideally in a mole ration of 1:2, to form an aqueous solution of magnesium bicarbonate.\|[0055] CO2 concentrations in exit gas were data-logged continuously. Occasional measurements of (fixed) inlet CO2 concentration were taken. The resulting data is shown in the two charts: one for day 1 detailing results 1200 (Fig. 12a) and one for day 2 detailing results 1201 (Fig 12b), 5 showing CO2 concentration (%CO2) versus time.\|[0056] Analysis: The total amount of CO2 removed from the inlet gas is calculated from the measured gas flow-rate and the measured difference between inlet and outlet gas concentration: \|[0057] Uncertainty in the flow-rate measurement (rotameter) is estimated from rotameter specifications as 3 %. The CO2 meter was able only to measure to the nearest 0.5 % in a CO2 concentration range of 0-5 %. Additionally, the inlet gas CO2 concentration from the pre-mix cylinder was measured at different times in the experiment as 4 % and 5 %. Absolute uncertainty in the measured % CO2 concentration change is estimated at 0.7 % CO2.\|[0058] The total amount of CO2 removed from the inlet gas during the 12 hour course of the experiment was measured as 1.87 moles (± 0.2 moles). Within experimental error, this is the amount of CO2 expected to be removed if all 0.871 moles of the initial Brucite had reacted with CO2 to form dissolved magnesium bicarbonate according to reaction (E7) above. Within the limits of measurements errors, results show that 100 % utilisation (carbonation) of Brucite is feasible when wet-scrubbing 5 % CO2-N2 gas mixture.\|[0059] Results also show that for the first 3.5 hours of the 12 hour experimental period, removal of CO2 from the inlet 5 % CO2-N2 gas mixture was 100 %. Over the first 6 hrs (first day), CO2 removal averaged 93 % and over the full 12 hours averaged 62%. Results show unequivocally that a Brucite-water suspension can fully scrub CO2 from dilute gas mixtures.\|[0060] It may be expected that in a future industrial CO2 scrubbing system, in which the rates of water, Brucite and CO2 addition may be controlled to maintain pH within a range of around pH 8 to pH 9, and where magnesium bicarbonate is removed, continuous removal of CO2, controllable up to 100%, should be possible and/or simultaneous with up to 100% conversion of Brucite to magnesium carbonates.\|[0061] Referring to "unpressurized" mentioned in the foregoing, it is optionally feasible to vent apparatus for implementing embodiments of the present disclosure directly to ambient atmosphere, namely substantially 1 Bar pressure, thereby avoiding a need for using expensive pressure vessels. However, optionally, embodiments of the present disclosure are operated in a substantially unpressurized manner at pressures in a range of 0.5 Bar to 10.0 Bar, more optionally in a range of 0.8 Bar to 5.0 Bar, and yet more optionally in a range of 0.9 Bar to 2.0 Bar. It will be appreciated that "pressurized", in contradistinction, refers to pressures, for example, in excess of 20 Bar, in excess of 50 Bar, or even in excess of 100 Bar.\|[0062] For example, the first steps of the process in which a mined magnesium silicate mineral is converted into magnesium hydroxide can be carried out at the mine site, while, without a need for elevated temperatures or pressures for reaction, the final step in which CO2 in flue-gas reacts with aqueous magnesium hydroxide, can be carried out at a distant source of CO2 emissions, such as a power station or on board a ship. Moreover, compared with magnesium silicate or the reaction mixture, magnesium hydroxide, having a lower molar mass and being able to react more completely with CO2, has a much higher CO2 sequestration capacity, namely tonnes of CO2 stored per tonne of magnesium hydroxide that is carbonated; this means that less material needs to transported and used to sequester the same mass of CO2 and, therefore, less energy and cost is expended in transport and handling tasks. In a non-inventive alternative embodiment, in which magnesium hydroxide powder is replaced with magnesium silicate powder in water slurry, it is surprisingly found, pursuant to the present disclosure, that it is also possible to achieve substantial direct aqueous-phase carbonation of Serpentine and Olivine powders, and substantial scrubbing of CO2 from ambient pressure flue gas. The prior art teaches that substantial and direct carbonation of Serpentine or Olivine powders is only possible under energy-intensive and costly conditions of elevated temperature or pressure, or with intense pre-processing, or with chemical additives. Pursuant to the present disclosure, it is found that high efficiency and low-cost non-inventive direct carbonation of Serpentine and Olivine can be achieved at ambient pressures and temperatures with only water or seawater and CO2 as additives in a simple carbonation reactor system. The CO2 can be pure or dilute, as in flue-gas or even in air, and at any partial pressure or temperature. In an embodiment of the present disclosure, there is injected simulated flue gas, namely a mixture of CO2 and N2, into a circulating slurry of the mineral powder in water and also in seawater. Many alternative gas-liquid mixing arrangements are possible, such as spraying of droplets solution of slurry into the gas. Similarly, many non-inventive alternative arrangements for solids-liquid mixing are possible, such as a fixed or stirred bed, or column of mineral particles through which water or brine is circulated to dissolve the mineral. By controlling a rate at which CO2 and/or mineral and/or water and/or energy are added or removed to/from the system, it was surprisingly found that conditions can be maintained in which the magnesium silicate mineral continuously dissolves and the CO2 is continuously scrubbed from the gas. Measurements of water containing Serpentine powder demonstrate an alkaline pH above pH8, and even above pH9. Serpentine and Olivine and other related magnesium silicate minerals such as chrysotile, lizardite, antigorite, and forsterite are composed of alternating crystal layers of magnesium oxide/hydroxide and silica. It is believed that the mechanism by which the magnesium silicate mineral dissolution and carbonation is possible under such mild conditions is that a suitable pH in the range of pH 8 to pH 9 is maintained by the addition of CO2, such that successive crystal layers of magnesium hydroxide dissolve directly into solution to form a solution of magnesium bicarbonate. In this pH range, carbonate ion concentration in solution is orders or magnitude lower than bicarbonate ion concentration and the formation of passivating solid magnesium carbonate phases on the surface of magnesium silicate particles is therefore avoided. Dissolution of the magnesium oxide layers is likely to destabilise the successive silica layers in the magnesium silicate crystal, so that the silica dissolves or precipitates as a solid, possibly accelerated by surface attrition due to stirring or solution circulation. The advantages pertaining to this surprising beneficial result of being able to carbonate magnesium silicate mineral powders according to a non-inventive process, namely without any pre-processing other than mining and crushing operations, directly under ambient conditions with just water and dilute CO2 are several, namely:\| (i) magnesium silicate mineral powders are much cheaper as feedstocks for carbonation than magnesium hydroxide, or thermally or chemically activated magnesium silicate mineral powers;\| (ii) carbonation can potentially be carried out directly at a huge scale at the site of the magnesium silicate mineral deposit using the CO2 available in air, or CO2 piped to the site, and with recirculation of water no additional water supply is needed;\| (iii) recovery and separation of pure CO2 gas and pure solid magnesium carbonate from the bicarbonate solution by conventional ageing, thermal or pressure-swing processes can provide compatibility with other CO2 transport, storage or utilisation options;\| (iv) separation of pure solid magnesium carbonate from bicarbonate solution provides a saleable chemical and industrial feedstock for other processes;\| (v) separation of silica solids from the dissolution/disintegration of the magnesium silicate mineral provides a further saleable industrial feedstock; and\| (vi) Nickel and Iron and other minor elemental constituents typically present in magnesium silicate minerals and wastes may be released in the process and can potentially be economically recovered from solution or by purification of the solid products.\|[0063] The efficiency of this entire process as illustrated in FIG. 1 and FIG.2 has been analysed through various scalability experiments, wherein it has been found that, for the Magnesium-mineral Silicates, the alkaline treatment is attractive as the associated Carbonation reaction is chemically favourable at a higher pH resulting in a higher reaction rate:\| Mg2SiO4 + 2NaOH +H2O => 2Mg(OH)2 (↓) +Na2SiO3 (aqueous) (8)\| Mg(OH)2 + CO2 => MgCO3 (↓) + H2O (9)\|[0064] In one of the embodiments, it is feasible to convert Dunite, an ultramafic rock rich in Magnesium-bearing minerals, into Magnesium Hydroxide (Mg(OH)2) by using highly concentrated Sodium Hydroxide (NaOH) aqueous solutions. The effect of the reaction time and the Sodium Hydroxide (NaOH) solution concentration on the process were studied to determine optimal conditions for achieving higher rate of conversion of Magnesium-mineral Silicates into Magnesium Hydroxide (Mg(OH)2). The product phases were identified by XRD and TG analysis. Careful quantification of Forsterite and Brucite both in raw materials and products were performed using Rietveld Refinement QPA and TG. The experimental results have been illustrated in the FIG. 3a and 3b FIG. 4a and 4b, FIG. 5, FIG. 6, Fig. 7a and 7b, FIG. 8, FIG. 9, FIG. 10, FIG. 11a and 11b; these results are indicated by 300, 301, 400, 401, 500, 600,700, 701, 800, 900, 1000, 1100, 1101 respectively. The experimental results of these drawings have been briefly elucidated in the foregoing.\|[0065] The tests conducted have shown that Magnesium-mineral Silicates constituting Dunite can be almost completely substituted with Brucite in highly concentrated solutions of Sodium Hydroxide (NaOH) and heated to a temperature of substantially 180 °C. According to the experimental results, increasing the Sodium Hydroxide (NaOH) concentration and the time of reaction are both factors that positively affect the conversion of Magnesium-Silicates into Magnesium Hydroxide. A greater amount of Magnesium Hydroxide (Mg(OH)2) was produced by using either a solution of Sodium Hydroxide (NaOH) having a molar concentration of 50 mol/kg for a temporal duration of 6 hours (73 wt%), or by using a solution of Sodium Hydroxide (NaOH) having a molar concentration of 40 mol/kg for a temporal duration of 18 and 24 hours (79 - 80 wt%). The TGA analyses results were found to be in accordance with the qualitative XRD results and with the Rietveld Refinement Quantitative Phase Analysis.\|[0066] During our exploration of optimal experimental conditions for different embodiments of the Olivine-NaOH reaction, we have discovered that it is possible to achieve substantial conversion of Olivine to Brucite in open vessels at ambient atmospheric pressure while heating to temperatures in the range 130-220 °C. At these elevated temperatures the vapour pressure of water significantly exceeds the reaction pressure. This discovery provides a significant advantage over the processes described by prior art systems in that the reaction can be conducted at much lower pressures (and even at ambient atmospheric pressure) using standard low-cost industrial reactors that typically are designed to withstand operating pressures up to 10 Bar.\|[0067] In accordance with another embodiment of the present invention, compacted Dunite powder can be heated in a sealed vessel at a temperature around 180°C, preferably for around six hours, to produce a product comprising Brucite.\|[0068] In accordance with another embodiment of the present invention, the Olivine and/or Serpentine is a Magnesium mineral which are suitable feedstock materials due to their high content of Magnesium (Mg) and wide abundance and large concentration in mineralogical sites.\|[0069] From the above description and claimed process, it will be appreciated that there is provided an improved process of alkali digestion for mineral Carbonation. The process can find utility in sequestration of Carbon Dioxide (CO2), extraction of valuable minerals, and other processes, known to the person skilled in the art, requiring the digestion of minerals for their Carbonation.\|[0070] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) comprises:\| reacting an alkaline earth silicate-based material with an alkali metal compound to form a mixture comprising a hydroxide of the alkaline earth, wherein the alkali metal is selected from sodium and/or potassium, and wherein the alkaline earth is selected from magnesium and/or calcium;\| reacting the mixture at a temperature in the range 140-220 °C and at a pressure of less than 10 Bar;\| separating the hydroxide of the alkaline earth from the mixture; and\| combining the hydroxide of the alkaline earth with a source of Carbon dioxide (CO2) producing a Carbonate or Bicarbonate or the alkaline earth. This gives a very beneficial production and sequestration of the hydroxide of the alkaline earth.\|[0071] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above further includes reacting the mixture in (b) at a pressure of less than the vapour pressure of pure water at the temperature of reaction.\|[0072] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above further includes using the mixture with a stoichiometric ratio between the Si in the alkaline earth silicate-based material and the alkali metal in the alkaline compound in a range of 1:1 to 1:2.\|[0073] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes using the mixture in a form of an aqueous solution with the molality of >30 molar of alkaline compound per litre water (H2O).\|[0074] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes reacting the mixture at ambient atmospheric pressure.\|[0075] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes executing the reaction at a temperature of ca 180 °C.\|[0076] Optionally, a non-inventive method of sequestration Carbon Dioxide (CO2) as outlined above includes using flue gases with less than 50vol% Carbon Dioxide (CO2) as part of a gas mixture for carbonation.\|[0077] Optionally, a non-inventive method of sequestrating Carbon Dioxide (CO2) as outlined above includes carrying out reactions in an unpressurised continuous mode to achieve substantially complete carbonation of the Magnesium Hydroxide or Magnesium silicate.\|[0078] Optionally, a non-inventive system for sequestrating Carbon Dioxide (CO2), wherein the system includes a first reaction chamber which is operable to receive a Silicate-based material and an alkaline compound, and a blending apparatus for blending contents of the first reaction chamber to produce a mixture therein.\|[0079] Optionally, the non-inventive system for sequestrating Carbon Dioxide (CO2) as described above is operable to execute the method outlined above method of sequestrating Carbon Dioxide (CO2).\|[0080] Modifications to embodiments of the invention described in the foregoing are possible without departing from the scope of the invention as defined by the accompanying claims. For example the compound in the reaction may be selected from any one or combination of Hydroxide, Carbonate, and/or Bicarbonate as would be suitable to the person skilled in the art. Expressions such as "including", "comprising", "incorporating", "consisting of", "have", "is used to describe and claim the present invention are intended to be construed in a non-exclusive manner, namely allowing for items, components or elements not explicitly described also to be present. Reference to the singular is also to be construed to relate to the plural. Numerals included within parentheses in the accompanying claims are intended to assist understanding of the claims and should not be construed in any way to limit subject matter claimed by these claims.	Family Number\|(45351908)\|45351908\|Object of Invention\|(EP3129125 B1)\|The present invention provides a method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, wherein the method comprises: a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from a group comprising alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole (...) \|Abstract\|(GB2516141 B)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) comprises heating a dry solid-solid mixture of magnesium silicate material with an alkali metal compound at a temperature below 300Â°C in an unpressurized vessel for less than 4 hours to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, and a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products. The magnesium silicate preferably comprises naturally occurring Olivine or Serpentine mineral. The magnesium hydroxide may be used to sequester carbon dioxide (CO2) to produce a metal carbonate.\|(WO2015154887 A1)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.\|(US9963351 B2)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300 C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.\|(EP3129125 B1)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.\|(CN106573197B B)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide ( CO2 ) is provided . The method includes heating a dry solid - solid mixture of an alkaline earth Silicate - based material with an alkali metal compound at a temperature below 300 C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate , wherein the Silicate - based material comprises a naturally occurring Olivine , Serpentine mineral and alkali metal silicate . The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry , comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide ( CO2 ) , producing a metal Carbonate . The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation . \|(DK3129125T T3)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300 C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.(From US9963351 B2)\|(ES2824676 T3)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300 C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.(From US9963351 B2)\|Advantages / Prev. Drawbacks\|(GB2515995 A)\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONALE RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flu Gases". \|(GB2516141 B)\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(GB2516141 A)\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(WO2015154887 A1)\|Moreover, similar problems with the approach are described in US patent application US2004126293A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(US9963351 B2)\|Moreover, similar problems with the approach are described in US patent application 2004126192A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(US20170029284 A1)\|Moreover, similar problems with the approach are described in US patent application 2004126192A1 (SHELL INTERNATIONAL RESEARCH), "Process for Removal and Capture of Carbon Dioxide from Flue Gases". \|(CN106573197B B)\|( . . . ) Therefore , there is a need to develop a carbon dioxide sequestration technology with higher energy efficiency , higher productivity , and higher cost efficiency than the prior art , and the technology can be applied to industrial production . \|(CN106573197 A)\|( . . . ) Therefore , there is a need to develop a carbon dioxide sequestration technology with higher energy efficiency , higher productivity , and higher cost efficiency than the prior art , and the technology can be applied to industrial production . \|Independent Claims\|(GB2516141 B)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal hydroxide to form a dry solid -solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid -solid mixture to a temperature below 300C (...) \|(GB2516141 A)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal compound to form a dry solid -solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid -solid mixture to a temperature below 300C (...) \|(WO2015154887 A1)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal compound to form a dry solid-solid mixture with a molar ratio in the range of 1 -3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300C (...) \|(US9963351 B2)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal hydroxide to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300 (...) \|(US20170029284 A1)\| (...) A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of alkali metal hydroxide to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per mole of silicon in the mixture; b. heating the dry solid-solid mixture to a temperature below 300 (...) \|(EP3129125 B1)\|1. A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide, comprising: a. mixing a dry powder of magnesium silicate rock with a dry powder of at least one alkali metal compound selected from the group consisting of alkali metal hydroxide, carbonates, bicarbonates, to form a dry solid-solid mixture with a molar ratio in the range of 1-3 moles of alkali metal per (...) \|(CN106573197B B)\|1. A process for activating magnesium silicate by conversion to magnesium hydroxide comprising the steps of : a . mixing the dried magnesium silicate rock powder with a dried alkali metal hydroxide powder , in a ratio of alkali metal elements in the alkali metal hydroxide : 1-3 mol of silicon element in the magnesium silicate is prepared into a dry solid mixture ; b . heating the dried solid mixture ( . . . ) \|(CN106573197 A)\|1. A process for activating magnesium silicate by conversion to magnesium hydroxide comprising the steps of : a . mixing the dried magnesium silicate rock powder with a dried alkali metal compound in a ratio of 1 : 3, preparing a dry solid mixture ; b . heating the dried solid mixture in a non - sealed pressurized container at a temperature below 300 ℃for up to 4 hours to form a glass phase mixture ( . . . ) \|	Chemical engineering\|Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-053/80\|B01D-2251/304\|B01D-2251/402\|B01D-2251/404\|B01D-2251/604\|B01D-2257/504\|B01D-2258/0283\|B01D-2259/126\|C01F-005/14\|C01F-005/22\|C01F-005/24\|C01F-011/12\|C01F-011/18\|C01P-2002/72\|C01P-2002/88\|Y02C-010/04\|Y02C-020/40\|Y02P-020/151\|Y02P-020/152		B01D-053/62\|B01D-053/80\|B01D-2251/304\|B01D-2251/402\|B01D-2251/404\|B01D-2251/604\|B01D-2257/504\|B01D-2258/0283\|B01D-2259/126\|C01F-005/14\|C01F-005/22\|C01F-005/24\|C01F-011/12\|C01F-011/18\|C01P-2002/72\|C01P-2002/88\|Y02C-010/04\|Y02C-020/40\|Y02P-020/151\|Y02P-020/152	B01D-053/62\|B01D-053/80\|B01F-003/18\|C01F-005/14\|C01F-005/22\|C01F-005/24\|C01F-011/12\|C01F-011/18	B01D-053/62\|B01D-053/80\|B01F-003/18\|C01F-005/14\|C01F-005/22\|C01F-005/24\|C01F-011/12\|C01F-011/18			CN109923068\|JP2025501392\|EP3743195\|WO2019145491;WO2019145491\|CN106365915\|CN106396746\|CN106396810\|WO201853497\|WO2025189212;WO2025189212\|CN119517198\|WO202530116\|CN115838261\|CN114560716\|EP4298057;EP4298057;EP4298057\|WO2023134849\|CN111715146\|CN111346600\|CN109734108\|CN111683732\|CN105457461\|CN105158439\|US20220127151\|US20190210883\|WO2024180441\|EP4421058\|US11896930\|US11718558\|US11718558\|US12110601\|US12110601\|US12559376\|EP3743195\|WO2019145491;WO2019145491\|FR3077008;FR3077008\|US11242261\|US10343113\|US9963351\|US9963351\|US9963351	CN109923068 85328121 WHO=Examiner SELF=N CAT=Y CAT=X\|JP2025501392 105792889 WHO=Examiner SELF=N CAT=Y\|EP3743195 85468981 WHO=Examiner SELF=N CAT=Y\|WO2019145491 85468981 WHO=Examiner SELF=N CAT=Y\|CN106365915 75280411 WHO=Examiner SELF=N CAT=Y\|CN106396746 75410669 WHO=Examiner SELF=N CAT=Y\|CN106396810 75410527 WHO=Examiner SELF=N CAT=Y\|WO201853497 85328121 WHO=Examiner SELF=N CAT=X CAT=Y\|WO2025189212 115804478 WHO=Examiner SELF=N CAT=A\|CN119517198 113515283 WHO=Examiner SELF=N CAT=A\|WO202530116 113238588 WHO=Examiner SELF=N CAT=A\|CN115838261 104347180 WHO=Examiner SELF=N CAT=A\|CN114560716 100272871 WHO=Examiner SELF=N CAT=A\|EP4298057 105792889 WHO=Examiner SELF=N CAT=A\|WO2023134849 105792889 WHO=Examiner SELF=N CAT=A\|CN111715146 90806865 WHO=Examiner SELF=N CAT=A\|CN111346600 89511061 WHO=Examiner SELF=N CAT=A\|CN109734108 84450910 WHO=Examiner SELF=N CAT=A\|CN111683732 85685129 WHO=Examiner SELF=N CAT=A\|CN105457461 72573513 WHO=Examiner SELF=N CAT=A\|CN105158439 71720639 WHO=Examiner SELF=N CAT=A\|US20220127151 85328121 WHO=Examiner SELF=N CAT=102 CAT=103\|US20190210883 85328121 WHO=Examiner SELF=N CAT=102 CAT=103\|WO2024180441 111220569 WHO=Applicant SELF=N\|EP4421058 111220569 WHO=Applicant SELF=N\|US11896930 104705306 WHO=Examiner SELF=N\|US11718558 92777983 WHO=Applicant SELF=N\|US11718558 92777983 WHO=Applicant SELF=N\|US12110601 86698390 WHO=Applicant SELF=N\|US12110601 86698390 WHO=Applicant SELF=N\|US12559376 85328121 WHO=Examiner SELF=N\|EP3743195 85468981 WHO=Applicant SELF=N\|WO2019145491 85468981 WHO=Applicant SELF=N\|FR3077008 85468981 WHO=Examiner SELF=N\|US11242261 85328121 WHO=Applicant SELF=N\|US10343113 72573513 WHO=Applicant SELF=N\|US9963351 45351908 WHO=Applicant SELF=Y\|US9963351 45351908 WHO=Applicant SELF=Y\|US9963351 45351908 WHO=Applicant SELF=Y	US5624493\|US5624493\|US4708640\|US4708640\|US8114374\|US8114374\|US20120288431\|US20120288431\|WO2015154887\|GB2516141\|US20150368154\|GB2515995\|CN102784570\|US20130036948\|US20130036948\|CN103415632\|US20120288431\|CN101830475\|CN101679059\|CN101679060\|CN101652323\|US8114374\|US8114374\|US7604787\|US20040213705\|US20040213705\|US20040213705\|US20040126293\|US5624493\|US5624493\|US4708640	US5624493 42940175 WHO=Examiner SELF=N CAT=X\|US5624493 42940175 WHO=Examiner SELF=N CAT=X\|US4708640 2618546 WHO=Examiner SELF=N CAT=X\|US4708640 2618546 WHO=Examiner SELF=N CAT=X\|US8114374 1759232 WHO=Examiner SELF=N CAT=A CAT=D\|US8114374 1759232 WHO=Examiner SELF=N CAT=A CAT=D\|US20120288431 1887580 WHO=Examiner SELF=N CAT=A\|US20120288431 1887580 WHO=Examiner SELF=N CAT=A\|WO2015154887 45351908 WHO=Applicant SELF=Y\|GB2516141 45351908 WHO=Applicant SELF=Y\|US20150368154 67252260 WHO=Examiner SELF=N\|GB2515995 45351908 WHO=Applicant SELF=Y\|CN102784570 7943846 WHO=Examiner SELF=N\|US20130036948 60642622 WHO=Applicant SELF=N\|US20130036948 60642622 WHO=Examiner SELF=N\|CN103415632 62236355 WHO=Examiner SELF=N\|US20120288431 1887580 WHO=Applicant SELF=N\|CN101830475 7095205 WHO=Examiner SELF=N\|CN101679059 1841774 WHO=Examiner SELF=N\|CN101679060 1841740 WHO=Examiner SELF=N\|CN101652323 6952466 WHO=Examiner SELF=N\|US8114374 1759232 WHO=Applicant SELF=N\|US8114374 1759232 WHO=Applicant SELF=N\|US7604787 43663450 WHO=Applicant SELF=N\|US20040213705 1759232 WHO=Applicant SELF=N\|US20040213705 1759232 WHO=Examiner SELF=N\|US20040213705 1759232 WHO=Examiner SELF=N\|US20040126293 793726 WHO=Applicant SELF=N\|US5624493 42940175 WHO=Applicant SELF=N\|US5624493 42940175 WHO=Examiner SELF=N\|US4708640 2618546 WHO=Applicant SELF=N		US4708640; US5624493; XP055204425; US20120288431; US8114374\|US4708640; US5624493; US20120288431; US8114374; US7604787; US20040126293; US8114374\|\|\|CN102784570; US5624493; CN101830475; CN101652323; CN103415632; CN101679059; CN101679060\|US20150368154; US4708640; US5624493; US8114374; US20040213705; US20120288431; US20130036948; GB2515995; GB2516141; WO2015154887\|US20130036948; US20040213705\|US20040213705	(EP3129125)\|Applicant references\|-The Masters thesis by Mabell Delgado Torróntegui at ETH in Switzerland, "Assessing the Mineral carbonation science and technology" (2010\|\|(US9963351)\|Search Report references [Examiner]\|-Zevenhoven et al., “Carbon dioxide mineralisation and integration with flue gas desulfurisation applied to a modern coal fired power plant,” Proceedings of ECOS 2012—Jun. 26-29, 2012, Perugia, Italy. (Year: 2012).\|-Combined Search and Examination Report received for the United Kingdom Patent Application No. GB1306559.4, dated Oct. 7, 2013, 6 pages.\|-Combined Search and Examination Report received for the United Kingdom Patent Application No. GB1406520.5, dated Nov. 11, 2014, 5 pages.\|-Examination Report received for the United Kingdom Patent Application No. GB1406520.5, dated Mar. 21, 2016, 2 pages.\|-International Search Report and Written Opinion received for International Patent Application No. PCT/EP2015/025018, dated Jul. 31, 2015, 10 pages.\|-Zevenhoven, Ron, et al., “Carbon Storage by Mineralisation (CSM): Serpentinite Rock Carbonation via Mg(OH)2 Reaction Intermediate without CO2 Pre-Separation”, Energy Procedia, Proceedings of the 11th International Conference on Greenhouse Gas Control Technologies GHGT-11, vol. 37, Dec. 2013, pp. 5945-5954.\|\|(WO2015/154887)\|International Search Report [Examiner]\|-RON ZEVENHOVEN ET AL: "Carbon Storage by Mineralisation (CSM): Serpentinite Rock Carbonation via Mg(OH)2 Reaction Intermediate Without CO2 Pre-separation", ENERGY PROCEDIA, vol. 37, 1 January 2013 (2013-01-01), pages 5945 - 5954, XP055204425, ISSN: 1876-6102, DOI: 10.1016/j.egypro.2013.06.521\|\|\|\|\|\|	GRANTED	(EP3129125)\|GRANTED\|(US9963351)\|GRANTED\|(WO2015/154887)\|LAPSED\|(GB2516141)\|LAPSED\|(GB2515995)\|LAPSED\|(CN106573197)\|GRANTED\|(ES2824676)\|GRANTED\|(DK3129125)\|LAPSED	ALIVE	(EP3129125)\|ALIVE\|(US9963351)\|ALIVE\|(WO2015/154887)\|DEAD\|(GB2516141)\|DEAD\|(GB2515995)\|DEAD\|(CN106573197)\|ALIVE\|(ES2824676)\|ALIVE\|(DK3129125)\|DEAD	(EP3129125)\|LEGAL DETAILS FOR EP3129125\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-04-10\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP15723131\|Application date=2015-04-10\|Standardized application number=2015EP-0723131\|Event publication date=2016-10-31\|Event 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FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IS\|MEMBER STATE LEGAL DETAILS FOR IT\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2025-04-22\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2025-04-22\|Year of payment of annual fees=11\|Corresponding cc:\|Designated or member state=IT\|MEMBER STATE LEGAL DETAILS FOR LI\|Actual or expected expiration date=2022-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LI\|Event publication date=2022-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting 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TIME-LIMIT\|Corresponding cc:\|Designated or member state=PT\|MEMBER STATE LEGAL DETAILS FOR RO\|Actual or expected expiration date=2021-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RO\|Event publication date=2021-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RO\|MEMBER STATE LEGAL DETAILS FOR RS\|Actual or expected expiration date=2021-02-26\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RS\|Event publication date=2021-02-26\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced 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fees payment date=2023-03-30\|Year of payment of annual fees=9\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2024-12-03\|Event code=EP/REG\|Event code=SE/EUG\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|EP patent has lapsed\|EUROPEISKT PATENT HAR UPPHOERT ATT GAELLA\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2025-10-13\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=SE\|MEMBER STATE LEGAL DETAILS FOR SI\|Actual or expected expiration date=2021-08-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SI\|Event publication date=2021-08-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SI\|MEMBER STATE LEGAL DETAILS FOR SK\|Actual or expected expiration date=2021-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SK\|Event publication date=2021-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SK\|MEMBER STATE LEGAL DETAILS FOR SM\|Actual or expected expiration date=2021-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SM\|Event publication date=2021-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SM\|MEMBER STATE LEGAL DETAILS FOR TR\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=TR\|Event publication date=2023-03-30\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2023-03-30\|Year of payment of annual fees=9\|Corresponding cc:\|Designated or member state=TR\|(US9963351)\|LEGAL DETAILS FOR US9963351\|Actual or expected expiration date=2035-07-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-04-10\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US15303208\|Application date=2015-04-10\|Standardized application number=2015US-15303208\|Event publication date=2015-04-10\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:ZIMMER, ANTHONY J\|Event publication date=2015-04-10\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2015-04-10\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: CCC001US\|Event publication date=2015-04-10\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 123123\|Event publication date=2015-04-10\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2015-04-10\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2016-10-10\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2016-10-10\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2016-10-17\|Event code=US/DISCSEF\|Event group=OAI\|Electronic Information Disclosure Statement\|Event publication date=2016-10-17\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2016-10-19\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2016-10-28\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2016-11-03\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2017-01-12\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2017-01-12\|Event code=US/M903\|Event indicator=Pos\|Event group=Examination events OAO\|Notice of DO/EO Acceptance Mailed\|Event publication date=2017-01-13\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2017-02-02\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20170029284\|Publication stage code=A1\|Publication date=2017-02-02\|Standardized publication number=US20170029284\|Event publication date=2017-02-02\|Event code=US/PGPUBN\|Event 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code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=2018-04-18\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2018-05-08\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US09963351\|Publication stage code=B2\|Publication date=2018-05-08\|Standardized publication number=US9963351\|Event publication date=2018-05-08\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 92 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=92\|Event publication date=2021-05-18\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2021-09-28\|Event code=US/MAFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|Maintenance Fee Payment\|Annual fees payment date=2021-09-28\|Year of payment of annual fees=4\|PAYMENT OF MAINTENANCE FEE, 4TH YR, SMALL ENTITY (ORIGINAL EVENT CODE: M2551)\|Entity status of patent owner: SMALL ENTITY\|Event publication date=2021-09-28\|Event code=US/M2551\|Event group=Payment or non-payment notifications\|Payment of Maintenance Fee, 4th Yr, Small Entity\|Event publication date=2025-05-20\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|Event publication date=2025-11-07\|Event code=US/M2552\|Event group=Payment or non-payment notifications\|Payment of Maintenance Fee, 8th Yr, Small Entity\|Event publication date=2025-11-07\|Event code=US/MAFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|Maintenance Fee Payment\|Annual fees payment date=2025-11-07\|Year of payment of annual fees=8\|PAYMENT OF MAINTENANCE FEE, 8TH YR, SMALL ENTITY (ORIGINAL EVENT CODE: M2552)\|Entity status of patent owner: SMALL ENTITY\|(WO2015/154887)\|LEGAL DETAILS FOR WO2015/154887\|Actual or expected expiration date=2017-10-10\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2015-04-10\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOEP2015/025018\|Application date=2015-04-10\|Standardized application number=2015WO-EP25018\|Event publication date=2015-10-15\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2015/154887\|Publication stage code=A1\|Publication date=2015-10-15\|Standardized publication number=WO2015154887\|Event publication date=2017-10-10\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR CN106573197\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN201580030663\|Application date in the designated or member state=2015-04-10\|Application number in the designated or member state=2015CN-80030663\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN106573197\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2017-04-19\|Publication number in the designated or member state=CN106573197\|Event publication date=2019-08-23\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2016-10-10\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2016-10-10\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR DK3129125\|Actual or expected expiration date=2024-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DK Corresponding appl: DK15723131\|Application date in the designated or member state=2015-04-10\|Application number in the designated or member state=2015DK-0723131\|Corresponding cc:\|Designated or member state=DK Corresponding pat: DK3129125\|Publication stage code in the designated or member state=T3\|Publication date in the designated or member state=2020-10-19\|Publication number in the designated or member state=DK3129125T\|Event publication date=2020-10-19\|Event code=DK/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=DK\|MEMBER STATE LEGAL DETAILS FOR EP3129125\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP15723131\|Application date in the designated or member state=2015-04-10\|Application number in the designated or member state=2015EP-0723131\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP3129125\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2017-02-15\|Publication number in the designated or member state=EP3129125\|Event publication date=2015-11-25\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2016-10-26\|Event code=WO/REEP\|Event indicator=Pos\|Event group=Entry into national phase\|Request for entry into the European phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2016-10-26\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2021-06-23\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR ES2824676\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=ES Corresponding appl: ES15723131\|Application date in the designated or member state=2015-04-10\|Application number in the designated or member state=2015ES-0723131T\|Corresponding cc:\|Designated or member state=ES Corresponding pat: ES2824676\|Publication stage code in the designated or member state=T3\|Publication date in the designated or member state=2021-05-13\|Publication number in the designated or member state=ES2824676\|Event publication date=2021-05-13\|Event code=ES/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=ES\|MEMBER STATE LEGAL DETAILS FOR US20170029284\|Actual or expected expiration date=2035-07-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=US Corresponding appl: US15303208\|Application date in the designated or member state=2015-04-10\|Application number in the designated or member state=2015US-15303208\|Corresponding cc:\|Designated or member state=US Corresponding pat: US20170029284\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2017-02-02\|Publication number in the designated or member state=US20170029284\|Event publication date=2016-10-10\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=US\|Event publication date=2025-05-20\|Event code=US/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=US\|(GB2516141)\|LEGAL DETAILS FOR GB2516141\|Actual or expected expiration date=2024-04-10\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2014-04-10\|Event code=GB/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=GB GB201406520\|Application date=2014-04-10\|Standardized application number=2014GB-0006520\|Event publication date=2014-05-28\|Event code=GB/D0\|Event indicator=Pos\|Event group=Examination events\|Patent application filed\|Publication country=GB\|Publication number=GB201406520\|Publication stage code=D0\|Publication date=2014-05-28\|Standardized publication number=GB201406520\|Event publication date=2015-01-14\|Event code=GB/A\|Event group=Examination events\|Published Application\|Publication country=GB\|Publication number=GB2516141\|Publication stage code=A\|Publication date=2015-01-14\|Standardized publication number=GB2516141\|Event publication date=2016-10-05\|Event code=GB/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent specification\|Publication country=GB\|Publication number=GB2516141\|Publication stage code=B\|Publication date=2016-10-05\|Standardized publication number=GB2516141\|Event publication date=2024-12-25\|Event code=GB/PCNP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent ceased through non-payment of renewal fee\|Effective date of the event=2024-04-10\|(GB2515995)\|LEGAL DETAILS FOR GB2515995\|Actual or expected expiration date=2018-02-21\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-04-10\|Event code=GB/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=GB GB201306559\|Application date=2013-04-10\|Standardized application number=2013GB-0006559\|Event publication date=2013-05-22\|Event code=GB/D0\|Event indicator=Pos\|Event group=Examination events\|Patent application filed\|Publication country=GB\|Publication number=GB201306559\|Publication stage code=D0\|Publication date=2013-05-22\|Standardized publication number=GB201306559\|Event publication date=2015-01-14\|Event code=GB/A\|Event group=Examination events\|Published Application\|Publication country=GB\|Publication number=GB2515995\|Publication stage code=A\|Publication date=2015-01-14\|Standardized publication number=GB2515995\|Event publication date=2018-02-21\|Event code=GB/WAP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application withdrawn, taken to be withdrawn or refused ** after publication under section 16(1)\|(CN106573197)\|LEGAL DETAILS FOR CN106573197\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-04-10\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201580030663\|Application date=2015-04-10\|Standardized application number=2015CN-80030663\|Event publication date=2017-04-19\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN106573197\|Publication stage code=A\|Publication date=2017-04-19\|Standardized publication number=CN106573197\|Event publication date=2017-04-19\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2017-05-17\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2019-08-23\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN106573197\|Publication stage code=B\|Publication date=2019-08-23\|Standardized publication number=CN106573197B\|Event publication date=2019-08-23\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|(ES2824676)\|LEGAL DETAILS FOR ES2824676\|Actual or expected expiration date=2035-04-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-04-10\|Event code=ES/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ES ES15723131\|Application date=2015-04-10\|Standardized application number=2015ES-0723131T\|Event publication date=2021-05-13\|Event code=ES/T3\|Event indicator=Pos\|Event group=Event indicating In Force\|Translation of granted European patent (former B3)\|Publication country=ES\|Publication number=ES2824676\|Publication stage code=T3\|Publication date=2021-05-13\|Standardized publication number=ES2824676\|(DK3129125)\|LEGAL DETAILS FOR DK3129125\|Actual or expected expiration date=2024-04-30\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2015-04-10\|Event code=DK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=DK DK15723131\|Application date=2015-04-10\|Standardized application number=2015DK-0723131\|Event publication date=2020-10-19\|Event code=DK/T3\|Event indicator=Pos\|Event group=Event indicating In Force\|Translation of EP patent\|Publication country=DK\|Publication number=DK3129125\|Publication stage code=T3\|Publication date=2020-10-19\|Standardized publication number=DK3129125T\|Event publication date=2024-11-25\|Event code=DK/REG\|Event code=DK/EBP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|EP PATENT LAPSED\|Ep patentet bortfaldet\|Effective date of the event=2024-04-30	(EP3129125)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2015/154887)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2015/154887)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2015/154887)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2015/154887)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2015/154887)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IR, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP3129125)\|EP; DE; ES; FR; GB; IT; NL; NO; TR\|(US9963351)\|US\|(WO2015/154887)\|CN; EP; ES; US\|(CN106573197)\|CN\|(ES2824676)\|ES	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=mswdBCXrAKbh9IrHURh/U2kyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP3129125&ekey=918&xpn=EP3129125&kind=B1	https://register.epo.org/application?number=EP15723131	https://permalink.orbit.com/RenderStaticFirstPage?XPN=OOZbZWp0GcLjCoOEB2EWlnfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	GB	(WO2015/154887)\|GB	(WO2015/154887)\|NAME=CAMBRIDGE CARBON CAPTURE LTD 3 Charles Babbage Road Cambridge, Cambridgeshire CB3 0GT , COUNTRY=GB	(EP3129125)\|GB\|(EP3129125)\|GB\|(WO2015/154887)\|GB\|\|	(EP3129125)\|NAME=Norris, Timothy Sweyn;Basck 50 - 60 Station Road , CITY=Cambridge CB1 2JH , COUNTRY=GB , REG=101324986\|(EP3129125)\|NAME=Norris, Timothy Sweyn;Basck 16 Saxon Road , CITY=Cambridge CB5 8HS , COUNTRY=GB , REG=101324986\|(WO2015/154887)\|NAME=NORRIS, Timothy Sweyn Basck 9 Meadowford Newport Saffron Walden, Essex CB11 3QL , COUNTRY=GB\|(CN106573197)\|NAME=ZHU HAIYAN;TAHOTA LAW FIRM , REG=51219\|(CN106573197)\|NAME=WANG SONGLAI;BEIJING CONCEPT INTELLECTUAL PROPERTY AGENCY	(EP3129125)\|GB\|(EP3129125)\|GB\|(US9963351)\|GB\|(US20170029284)\|GB\|(WO2015/154887)\|GB\|\|\|\|(CN106573197)\|GB\|\|\|	(EP3129125)\|NAME=PRIESTNALL, Michael 3 Charles Babbage Road, CITY=CambridgeCambridgeshire CB3 0GT, COUNTRY=GB\|(EP3129125)\|NAME=PRIESTNALL, Michael 3 Charles Babbage Road, CITY=CambridgeCambridgeshire CB3 0GT, COUNTRY=GB\|(US9963351)\|NAME=Priestnall Michael, CITY=Cambridge, COUNTRY=GB\|(US20170029284)\|NAME=PRIESTNALL Michael, CITY=Cambridge, COUNTRY=GB\|(WO2015/154887)\|NAME=PRIESTNALL, Michael 3 Charles Babbage Road Cambridge, Cambridgeshire CB3 0GT, COUNTRY=GB\|(GB2516141)\|NAME=Michael Priestnall\|(GB2516141)\|NAME=MICHAEL PRIESTNALL\|(GB2515995)\|NAME=MICHAEL PRIESTNALL\|(CN106573197)\|NAME=Michael. Stena Plymouth The British Cambridge County of Cambridge city Charles Babbage Road No. 3, CITY=Cambridge, STATE=Cambridgeshire , COUNTRY=GB\|(CN106573197)\|NAME=PRIESTNALL MICHAEL\|(ES2824676)\|NAME=PRIESTNALL, Michael\|(DK3129125)\|NAME=PRIESTNALL, Michael	(WO2015/154887)\|11\|(EP3129125)\|12\|(CN106573197)\|12\|(US9963351)\|12\|(GB2516141)\|12\|(GB2515995)\|11	3	8			(EP3129125)\|WO2015/154887\|(US9963351)\|WO2015/154887\|(CN106573197)\|WO2015/154887\|(ES2824676)\|WO2015/154887\|(DK3129125)\|WO2015/154887	(ES2824676)\|EP15723131\|(DK3129125)\|EP15723131	(EP3129125)\|Number of Claims: NCL=11\|\|(US9963351)\|Number of Claims: NCL=14\|Number of Drawings: NDR=16\|Number of Figures: NFG=17\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=92\|Primary examiner: Zimmer Anthony J\|Art Unit.: ART =1736\|\|(US20170029284)\|Number of Claims: NCL=14\|Number of Drawings: NDR=16\|Number of Figures: NFG=17\|Independent Claim Number: ICL=14\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=14\|Primary examiner: Zimmer Anthony J\|Art Unit.: ART =1736\|\|(WO2015/154887)\|Number of Claims: NCL=13\|Extended kind: EXTK=x\|\|(GB2516141)\|Number of Claims: NCL=11\|\|(GB2516141)\|Number of Claims: NCL=13\|\|(GB2515995)\|Number of Claims: NCL=9\|\|(CN106573197)\|Number of Claims: NCL=11\|Gazette date: GAZDATE=2019-08-23\|Gazette number: GAZNUM=35-3402\|Substantial examination effective date: 20170517 Examination duration: 27 months\|Number of Pages: NPAGES=32\|Primary examiner: 王如军\|Primary examiner: Wang Ru Jun\|\|(CN106573197)\|Number of Claims: NCL=13\|Gazette date: GAZDATE=2017-04-19\|Gazette number: GAZNUM=33-16\|Substantial examination effective date: 20170517 Examination duration: 27 months\|Number of Pages: NPAGES=31\|Primary examiner: 王如军\|Primary examiner: Wang Ru Jun\|	(US9963351)\|Previous publication: US20170029284 A1 2017-02-02 [US20170029284]\|(CN106573197)\|Previous publication: CN106573197 A 2017-04-19 [CN106573197]	(EP3129125)\|ENGLISH (ENG)	(ES2824676)\|Patent\|(DK3129125T)\|Patent\|(EP3129125)\|Patent\|(CN106573197B)\|Patent\|(US9963351)\|Patent\|(CN106573197)\|Patent\|(EP3129125)\|Patent\|(US20170029284)\|Patent\|(GB2516141)\|Patent\|(WO2015154887)\|Patent\|(GB2515995)\|Patent\|(GB2516141)\|Patent\|(GB201406520)\|Patent\|(GB201306559)\|Patent	Titre: (EP3129125)\|Method of activation of mineral silicate minerals Résumé: (EP3129125)\|A method for activation of magnesium silicate minerals by conversion to magnesium hydroxide for sequestration of carbon dioxide (CO2) is provided. The method includes heating a dry solid-solid mixture of an alkaline earth Silicate-based material with an alkali metal compound at a temperature below 300C to form a solid product predominantly comprising a mixture of magnesium hydroxide and alkali metal silicate, wherein the Silicate-based material comprises a naturally occurring Olivine, Serpentine mineral and alkali metal silicate. The method includes a subsequent dissolution of the solid product in aqueous solution to form an alkaline aqueous liquid slurry, comprising solid and aqueous phase products and the reaction of the solid phase thus formed with Carbon Dioxide (CO2), producing a metal Carbonate. The method provides a process that has shown significant cost and energy efficiencies for producing magnesium hydroxide and CO2 sequestration via mineral carbonation.	21	Abstract	gpt-4o-mini	yes	The article describes a method for activating silicate minerals to sequester CO2 through mineral carbonation, which aligns with the topic of enhanced weathering.
23	CN202310871419	CN202310871419	CN116808978	106692037	CN116808978 A 2023-09-29 [CN116808978]	2023-07-17	2023-07-17	2023-09-29		(CN116808978)\|2025-02-21	(CN116808978)\|Kettle-type reaction device for carbonization test of building materials and application of kettle-type reaction device	(CN116808978)\|The invention provides a kettle type reaction device for a carbonization test of a building material. The kettle type reaction device comprises an airtight reaction tank body, a temperature adjusting device, a humidity adjusting device, an air pressure adjusting device, a carbon dioxide gas input device and a sensor group. The invention further provides a building material carbonization test system. The building material carbonization test system comprises the kettle type reaction device and a control center. The invention also provides an application of the building material carbonization test system in researches such as consumption of carbon dioxide waste gas, carbon immobilization in a deep ground environment, rock weathering or CO2 mineralization and the like. The building material carbonization test system disclosed by the invention has higher safety when being used for high-concentration carbonization test of the building material, the test result is more in line with the real situation, and the carbon absorption or carbon resistance of the building material under the condition of high-concentration carbon dioxide can be measured under normal pressure; the method has higher reference value for research on consumption of carbon dioxide waste gas, carbon immobilization of deep ground environment, rock weathering or CO2 mineralization and the like.	NELD INTELLIGENT TECHNOLOGY XIANGHE	(CN116808978)\|NELD INTELLIGENT TECHNOLOGY XIANGHE CO., LTD. ([CN])	ZHANG HUIYI	(CN116808978)\|ZHANG HUIYI	(CN116808978)\|LIU JUNLING;BEIJING ZHAOJUN UNION INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11333	(CN116808978)\|On the one hand, the concrete is not easy to breathe, because the binding degree of the cementing material, sand and stones in the concrete is higher after hydration reaction, the higher the strength is, the stronger the inner compactness of the concrete is, and the through holes are hardly formed, so that the outside air is difficult to smoothly diffuse into the inside of the concrete.\|	(CN116808978)\|1. A kettle reaction device for carbonization testing of building materials, comprising:the airtight reaction tank body is used as an airtight space for accommodating a test block and forming a preset environment of carbon dioxide concentration, temperature, air pressure and humidity;the temperature adjusting device is arranged in the airtight reaction tank body and used for adjusting the temperature in the airtight reaction tank body;the humidity adjusting device is used for adjusting the humidity in the airtight reaction tank body;the air pressure adjusting device is arranged on the airtight reaction tank body and is used for adjusting the air pressure in the airtight reaction tank body;the carbon dioxide gas input device is used for externally connecting carbon dioxide storage equipment and inputting carbon dioxide gas into the airtight reaction tank body;and the sensor group is used for monitoring the concentration, temperature, air pressure and humidity of the carbon dioxide in the airtight reaction tank body.\|	(CN116808978)\|A further object of the invention is: provides the kettle type reaction device for consuming carbon dioxide waste gas generated by cement plants or power plants, carbon solid storage in deep environment, rock efflorescence and CO by cement building materials 2 Mineralization and other research applications. The above object of the present invention is achieved by the following means: in a first aspect, the present invention provides a tank reactor for carbonization testing of building materials, comprising:\|The invention provides a kettle type reaction device for a carbonization test of building materials, which comprises: the device comprises an airtight reaction tank body, a temperature adjusting device, a humidity adjusting device, an air pressure adjusting device, a carbon dioxide gas input device and a sensor group. The invention also provides a carbonization test system for the building material, which comprises the kettle-type reaction device and a control center. The invention also provides the building material carbonization test system for carbon sequestration and rock weathering or CO in the deep environment consuming carbon dioxide waste gas 2 Mineralization and other research applications.\|The invention relates to a kettle type reaction device capable of providing high-concentration carbon dioxide, which uses carbon dioxide waste gas to carry out inorganic building material maintenance, carbon sequestration in deep environment, rock weathering and CO 2 Mineralization and other research applications.\|	(CN116808978)\|AIRTIGHT REACTION TANK(100,82)\|BUILDING MATERIAL(100,71)\|KETTLE TYPE REACTION(100,20)\|KETTLE REACTION(100,16)\|CARBONIZATION(100,10)\|BUILDING MATERIAL TESTING(100,2)\|REACTION TANK(60,71)\|TANK REACTOR(40,11)\|DEEP ENVIRONMENT(36,7)\|HUMIDITY(34,21)\|MINERALIZATION(34,7)\|CONCRETE CARBONIZATION TESTING(30,1)\|CONCRETE INNER COMPACTNESS(30,1)\|CARBON DIOXIDE(25,103)\|CONCRETE CARBONATION TEST(25,1)\|CIRCULATION PROMOTION(22,1)\|REGULATING HUMIDITY(22,1)\|PRESET DEVICE ENVIRONMENT(21,2)\|TOUCHSCREEN(20,9)\|CARBONIZATION TEST(20,5)\|INNER COMPACTNESS(20,1)\|PUTTING STEAM(19,1)\|CONCRETE(18,15)\|PRESSURIZED NITROGEN INLET(18,1)\|CARBON SEQUESTRATION(17,7)\|INVENTIONTHE MATERIAL CARBONIZATION(17,1)\|CARBON DIOXIDE CONCENTRATION SENSOR(16,16)\|SENSOR GROUP(16,5)\|CARBON DIOXIDE PRESET ENVIRONMENT(16,2)\|GAS INPUT(15,11)\|CARBON DIOXIDE WASTE GAS(15,9)\|EFFLORESCENCE(15,2)\|AIRTIGHT SPACE(14,4)\|CARBON DIOXIDE GAS INPUT(12,11)\|CARBON DIOXIDE GAS(12,10)\|WASTE GAS(12,9)\|CEMENT PLANT(12,4)\|ELECTROMAGNETIC VALVE(12,4)\|BUILDING MATERIAL CARBONIZATION TEST(12,1)\|STEAM INPUT(12,1)\|CARBONIZATION TEST SYSTEM(11,27)\|HUMIDITY SENSOR(11,10)\|PRESET PARAMETER CONDITION(11,3)\|STORAGE EQUIPMENT(11,3)\|CEMENT KILN FLUE GAS(11,2)\|CARBON SOLID STORAGE(11,1)\|HYDRATION REACTION(11,1)\|SAND(11,1)\|TEST CARBON ABSORPTION PERFORMANCE(11,1)\|BLOWER(10,2)\|CARBON CURING(10,2)\|EVAPORATOR(10,2)\|TEST BLOCK(9,11)\|HEATING ROD(9,6)\|CARBON DIOXIDE STORAGE EQUIPMENT(9,3)\|MAN MACHINE INTERACTION INTERFACE(9,3)\|TRAPPING(9,2)\|OUTSIDE AIR(9,1)\|CARBON MONOXIDE(8,20)\|STEAM GENERATOR(8,1)\|FAN WIND WHEEL(7,6)\|MINERALIZATION RESEARCH(7,2)\|TEMPERATURE ADJUSTMENT(7,2)\|BUILDING MATERIAL MAINTENANCE(7,1)\|AIR PRESSURE(6,26)\|HUMIDITY MEASUREMENT(6,3)\|PRESET VALUE(6,3)\|VACUUMIZING TUBE(6,3)\|CEMENT BUILDING MATERIAL(6,2)\|CURING(6,2)\|PRESSURE REDUCTION(6,1)\|INNER CONTAINER(5,13)\|PRESSURE SENSOR(5,10)\|TEMPERATURE SENSOR(5,10)\|POWER PLANT(5,6)\|CARBON DIOXIDE INPUT(5,3)\|AIR PRESSURE REGULATOR(5,1)\|CARBONATION TEST SYSTEM(5,1)\|CARBONIZATION TEST KETTLE REACTOR(5,1)\|CEMENTING MATERIAL(5,1)\|VACUUM PUMP(5,1)\|LINER(4,9)\|CONCRETE TEST BLOCK(4,5)\|CARBON DIOXIDE CONCENTRATION MEASUREMENT(4,3)\|AIR COMPRESSOR(4,2)\|BUILDING MATERIAL CARBON MAINTENANCE(4,2)\|RAPID REACTION(4,2)\|ACCELERATED WEATHERING(4,1)\|CARBONATION DEPTH(4,1)\|CARBONTHE RESEARCH(4,1)\|CEMENT ROCK(4,1)\|CEMENTING MATERIAL DEGREE(4,1)\|CONCRETE LATE STRENGTH(4,1)\|FACTOR RESEARCHING INFLUENCE(4,1)\|GEOLOGICAL SEALING(4,1)\|INFLUENCE CARBONIZATION(4,1)\|LABORATORY EQUIPMENT PERSONNEL QUALIFICATION(4,1)\|OPERATOR SKILL QUALIFICATION(4,1)\|RESEARCHER(4,1)\|VACUUMIZING PIPE(4,1)\|CONTROL CENTER(3,10)\|HIGH CONCENTRATION CARBONIZATION(3,5)\|INNER TANK(3,4)\|BAROMETER(3,3)\|HYGROMETER(3,3)\|TEMPERATURE MEASUREMENT(3,3)\|TEST RESULT(3,3)\|THERMOMETER(3,3)\|CARBON DIOXIDE CONCENTRATION METER(3,2)\|CEMENT FACTORY(3,2)\|CLOSED CONTAINER(3,2)\|DECOMPRESSION(3,2)\|CARBONIZATION BOX(3,1)\|CARBONIZATION DEPTH(3,1)\|EVACUATION PIPE(3,1)\|GEOLOGICAL STORAGE(3,1)\|TEMPERATURE REDUCTION(3,1)\|CONTROL UNIT(2,12)\|HIGH CONCENTRATION CARBON DIOXIDE(2,5)\|INTEGRATED CIRCUIT CHIP(2,4)\|OUTER SHELL(2,4)\|OUTER TANK(2,4)\|CARBON DIOXIDE ABSORPTION CAPACITY(2,3)\|CONTROL CABINET(2,3)\|DATA PROCESSING(2,3)\|PRESSURE MEASUREMENT(2,3)\|LIQUID DISCHARGE(2,2)\|ABSORBING CARBON DIOXIDE(2,1)\|CARBON COLLECTION(2,1)\|CARBON NEUTRALIZATION(2,1)\|CEMENT PRODUCTION(2,1)\|CONCENTRATION TECHNICAL MEASURE(2,1)\|CONCENTRATIONAND(2,1)\|CONCRETE CARBON DIOXIDE ABSORPTION(2,1)\|CONCRETE CARBON RESISTANCE(2,1)\|DAMP ADJUSTMENT(2,1)\|DEEP SOIL ENVIRONMENT(2,1)\|EVACUATING TUBE(2,1)\|HUMIDITY ENVIRONMENT(2,1)\|RAPID EVALUATION(2,1)\|REFRIGERATION(2,1)\|SLEEVED INSIDE(2,1)\|TECHNICAL GRADE(2,1)\|VACUUMIZING GAS(2,1)\|	(CN116808978)\|1. A kettle reaction device for carbonization testing of building materials, comprising:\|the airtight reaction tank body is used as an airtight space for accommodating a test block and forming a preset environment of carbon dioxide concentration, temperature, air pressure and humidity;\|the temperature adjusting device is arranged in the airtight reaction tank body and used for adjusting the temperature in the airtight reaction tank body;\|the humidity adjusting device is used for adjusting the humidity in the airtight reaction tank body;\|the air pressure adjusting device is arranged on the airtight reaction tank body and is used for adjusting the air pressure in the airtight reaction tank body;\|the carbon dioxide gas input device is used for externally connecting carbon dioxide storage equipment and inputting carbon dioxide gas into the airtight reaction tank body;\|and the sensor group is used for monitoring the concentration, temperature, air pressure and humidity of the carbon dioxide in the airtight reaction tank body.\|2. The kettle type reaction device as claimed in claim 1, wherein said temperature adjusting device is composed of a heating device and a refrigerating device; the heating device is a heating rod; the refrigerating device is an evaporator or a plate heat exchanger.\|3. The tank reactor according to claim 2, wherein the humidity regulator is a steam input device provided in the airtight reaction tank, and the humidity is increased by inputting steam into the airtight reaction tank via an external steam generator.\|4. The tank reactor of claim 3 wherein said air pressure regulator comprises a vacuum pump, an air compressor and/or a pressurized nitrogen inlet.\|5. The tank reactor according to any one of claims 1 to 4, wherein a blower means is provided in the airtight reaction tank for promoting circulation of gas in the airtight reaction tank.\|6. The tank reactor of claim 5 wherein said sensor set comprises a carbon dioxide concentration sensor, a temperature sensor, a pressure sensor and a humidity sensor; the temperature sensor, the pressure sensor and the humidity sensor are arranged on the airtight reaction tank body and are used for directly contacting the gas in the airtight reaction tank body; the carbon dioxide concentration sensor is arranged inside or outside the airtight reaction tank body, the carbon dioxide concentration sensor arranged inside the airtight reaction tank body is used for directly contacting the gas with the temperature lower than 50 ℃ in the airtight reaction tank body, and the carbon dioxide concentration sensor arranged outside the airtight reaction tank body is used for contacting the gas which is collected from the airtight reaction tank body and is subjected to temperature reduction and pressure reduction.\|7. A building material carbonization test system, characterized in that: comprising a tank reactor and a control center according to any one of claims 1 to 6; the control center is provided with a temperature measurement and control unit, a humidity measurement and control unit, a pressure measurement and control unit and a carbon dioxide concentration measurement and control unit, wherein each measurement and control unit respectively receives signals or data from the temperature sensor, the humidity sensor, the pressure sensor and the carbon dioxide concentration sensor, and controls the operation of the temperature adjusting device, the humidity adjusting device, the air pressure adjusting device, the carbon dioxide input device and the fan device of the kettle type reaction device through a control circuit and an electromagnetic valve, so that the airtight reaction tank body of the kettle type reaction device achieves preset parameter conditions.\|8. The building material carbonization test system according to claim 7, wherein: the control center is also provided with an integrated circuit chip and a touch screen; the touch screen can display a man-machine interaction interface, is used for displaying operation state parameters of the kettle type reaction device to an operator, and is used for inputting parameters and instructions by the operator; the integrated circuit chip utilizes an embedded program to complete data processing and control of each measurement and control unit and the touch screen.\|9. Use of the carbonization testing system for concrete carbonization testing building material according to any one of claims 7 or 8 for high concentration carbonization testing of building material, characterized in that: placing a building material test block in an airtight reaction tank body of a kettle-type reaction device of a building material carbonization test system, firstly vacuumizing the airtight reaction tank body to negative pressure through a vacuumizing device of the kettle-type reaction device, rapidly filling carbon dioxide gas into the airtight reaction tank body through a pressurized carbon dioxide gas input device of the kettle-type reaction device, enabling the air pressure in the airtight reaction tank body to reach normal pressure and the carbon dioxide concentration to reach more than 90%, and then adjusting the temperature, humidity and air pressure in the airtight reaction tank body to reach preset values through a temperature adjusting device, a humidity adjusting device and an air pressure adjusting device of the kettle-type reaction device based on detection of a sensor group of the kettle-type reaction device, and observing the carbon absorption performance of the test block according to a conventional method.\|10. Use of the concrete carbonation test building material carbonation test system according to any one of claims 7 or 8 and for consuming carbon dioxide waste gas generated by a cement plant or a power plant, characterized in that: the building material carbonization test system is used for carbon maintenance of building materials; the method specifically comprises the following steps: CO of cement kiln flue gas 2 After trapping, carbon dioxide gas is input into the airtight reaction tank body through the carbon dioxide gas input device of the carbonization test system for building materials according to any one of claims 7 or 8 to carry out carbon curing on the building materials, and the curing process is completed by carrying out constant pressure rapid reaction at the pressure of 1bar-15bar and the normal temperature for 2 hours.	(CN116808978)\|TECHNICAL FIELD\|[0001] The invention relates to a kettle type reaction device capable of providing high-concentration carbon dioxide, which uses carbon dioxide waste gas to carry out inorganic building material maintenance, carbon sequestration in deep environment, rock weathering and CO 2 Mineralization and other research applications.\|BACKGROUND ART\|[0002] "Green" low carbonThe research and development of cement production technology, namely low-carbon/ultra-low-carbon concrete in the field of building materials, is a hot spot of research and development at the present stage. Meanwhile, in view of the fact that the carbon dioxide is absorbed and utilized by the concrete after being captured, the strength of the concrete can be greatly improved, so that how to achieve carbon neutralization and improve the strength of building materials in the building material industry is a new hot spot for research in the industry. Furthermore, for technical grade CO 2 The carbon collection and deep-ground carbon sequestration technology is also of great significance for realizing 'double carbon targets', wherein factors such as deep-ground environment temperature, pressure and the like influence carbonization rules and CO in different stratum environments 2 The problems of stability, temperature, pressure and the like are worthy of intensive research.\|[0003] In the development of "carbon-neutral" production technology and deep-ground carbon sequestration technology for building materials, in particular inorganic building materials, research into carbonization of concrete has been involved. The carbonization of concrete means that carbon dioxide in air and calcium hydroxide in cement stone are subjected to chemical action under the condition of existence of water to generate calcium carbonate and water. The carbonization process is a process that carbon dioxide gradually diffuses from the surface to the inside of the concrete. The most important effect of carbonization on concrete is: the early strength and the later strength of the concrete are improved rapidly, the deeper the carbonization depth is, the higher the strength of the concrete is, and the different carbon dioxide absorption capacities of different mixing ratios of the concrete can be embodied through the carbonization process. In order to match with the consumption of carbon dioxide waste gas, the CO of the concrete under the high-temperature and high-pressure conditions in the research and development of being absorbed by the concrete and the geological storage technology 2 The carbon absorption and carbon resistance of the concrete are required to be detected through a carbonization test.\|[0004] The alkaline component in the concrete material can be mixed with CO with the concentration of 0.04% in the atmosphere under the natural condition 2 The chemical reaction is carried out but the process is very slow, with the depth of carbonation generally "no more than" 10 mm over its life cycle. But can quickly realize concrete carbonization by the technical measures of concentration improvement, temperature rise, pressurization and the like, and the strength of the product is higher. In the prior art, the carbonization test process of concrete generally comprises the steps of delivering carbon dioxide-containing gas with a certain concentrationAnd (3) placing the sample into a closed container for holding the concrete test block, and observing the depth of carbon dioxide absorbed by the test block or permeated and diffused into the test block within a certain time. For the study of carbon dioxide absorption of concrete, the carbonization test for measuring carbon absorption performance thereof requires the use of high concentration carbon dioxide gas. In the current practice, a high-concentration high-pressure high-temperature carbonization box is used for concrete carbonization test, high-concentration carbon dioxide is pressed into concrete by using the pressure of high-pressure gas, and the absorption and neutralization effects of the concrete on the carbon dioxide are observed. The high pressure of the gas in this test is usually generated by charging a large amount of carbon dioxide gas into a closed container containing air in order to achieve a sufficiently high carbon dioxide concentration, and the gas is also used by the test person as a driving force for absorbing carbon dioxide in concrete. However, such high pressure tests not only require a high pressure resistant container, but also have special requirements for the skill qualification of the operators, which would otherwise present a significant production safety risk.\|DISCLOSURE\|Disclosure of Invention\|[0005] In view of the above technical background, a primary object of the present invention is: the kettle type reaction device for the carbonization test of the building material can provide a high-concentration carbon dioxide environment and has higher safety.\|[0006] A further object of the invention is: provides the kettle type reaction device for consuming carbon dioxide waste gas generated by cement plants or power plants, carbon solid storage in deep environment, rock efflorescence and CO by cement building materials 2 Mineralization and other research applications.\|[0007] The above object of the present invention is achieved by the following means:\|in a first aspect, the present invention provides a tank reactor for carbonization testing of building materials, comprising:\|the airtight reaction tank body is used as an airtight space for accommodating a test block and forming a preset environment of carbon dioxide concentration, temperature, air pressure and humidity;\|the temperature adjusting device is arranged in the airtight reaction tank body and used for adjusting the temperature in the airtight reaction tank body;\|the humidity adjusting device is used for adjusting the humidity in the airtight reaction tank body;\|the air pressure adjusting device is arranged on the airtight reaction tank body and is used for adjusting the air pressure in the airtight reaction tank body;\|the carbon dioxide gas input device is used for externally connecting carbon dioxide storage equipment and inputting carbon dioxide gas into the airtight reaction tank body;\|and the sensor group is used for monitoring the concentration, temperature, air pressure and humidity of the carbon dioxide in the airtight reaction tank body.\|[0008] In the tank reactor according to the present invention, the size, shape and material of the airtight reaction tank are not particularly limited, but it is necessary to have airtightness to maintain the pressure and concentration of the internal gas and to have a certain strength to avoid deformation due to the pressure difference between the inside and outside thereof.\|[0009] In the kettle-type reaction device, the temperature adjusting device consists of a heating device and a refrigerating device; the heating device can be a heating rod and the like; the refrigeration device may be an evaporator or the like.\|[0010] In the kettle-type reaction device, the humidity adjusting device is a water vapor input device arranged on the airtight reaction tank body, and water vapor is input into the airtight reaction tank body through an external water vapor generating device to increase the humidity.\|[0011] In the kettle-type reaction device, the air pressure adjusting device at least comprises a vacuumizing device. In a further preferred scheme, the air pressure adjusting device can further comprise an external air compressor, a nitrogen input device with pressure and the like.\|[0012] In the tank reactor according to a further preferred aspect of the present invention, a blower device is provided in the airtight reaction tank to promote circulation of the gas in the airtight reaction tank in order to uniformly mix the gas in the airtight reaction tank.\|[0013] In the kettle-type reaction device, the sensor group comprises a carbon dioxide concentration sensor, a temperature sensor, a pressure sensor and a humidity sensor. The temperature sensor, the pressure sensor and the humidity sensor are arranged on the airtight reaction tank body and are used for directly contacting the gas in the airtight reaction tank body; the carbon dioxide concentration sensor is arranged inside or outside the airtight reaction tank body, the carbon dioxide concentration sensor arranged inside the airtight reaction tank body is used for directly contacting the gas with the temperature lower than 50 ℃ in the airtight reaction tank body, and the carbon dioxide concentration sensor arranged outside the airtight reaction tank body is used for contacting the gas which is collected from the airtight reaction tank body and is subjected to cooling and decompression after the gas with the temperature higher than 50 ℃ is collected.\|[0014] In a preferred embodiment of the present invention, the inner space of the airtight reaction tank is divided into two communicating areas: the test block placing area and the gas mixing area; the test block placing area is used for intensively placing one or more than two test blocks, the sensor group is directly contacted with the gas of the test block placing area, and the vacuumizing device is used for vacuumizing the gas of the test block placing area; the gas mixing area is used for receiving water vapor and carbon dioxide gas from the outside of the airtight reaction tank body and heating the gas, the temperature adjusting device is arranged in the gas mixing area, and the water vapor input device and the carbon dioxide gas input device are both opened in the gas mixing area.\|[0015] In a preferred embodiment of the present invention, in order to better reduce heat dissipation by conduction from the inside of the airtight reaction tank to the outside, the airtight reaction tank is composed of an inner tank and an outer tank, the inner tank is nested in the outer tank, and a gap is left between the inner tank and the outer tank. In a more preferable scheme, the inner tank body and the outer tank body are fixedly connected through a plurality of devices which are mutually connected in a screwed mode.\|[0016] In a further preferred scheme of the invention, in order to more flexibly adjust the air pressure and the carbon dioxide concentration in the airtight reaction tank body, the airtight reaction tank body is also provided with a nitrogen or air input device; in a more preferred embodiment, the nitrogen or air inlet means is open to the gas mixing zone.\|[0017] In a further preferred scheme of the invention, the airtight reaction tank body is also provided with an exhaust device and a liquid discharge device which are used for discharging gas and liquid in the airtight reaction tank body.\|[0018] In a further preferred scheme of the invention, the airtight reaction tank body is also provided with a safety valve.\|[0019] On the basis, the invention also provides a carbonization test system for building materials, which comprises the kettle-type reaction device and a control center; the control center is provided with a temperature measurement and control unit, a humidity measurement and control unit, a pressure measurement and control unit and a carbon dioxide concentration measurement and control unit, wherein each measurement and control unit respectively receives signals or data from the temperature sensor, the humidity sensor, the pressure sensor and the carbon dioxide concentration sensor, and controls the operation of the temperature adjusting device, the humidity adjusting device, the air pressure adjusting device, the carbon dioxide input device and the fan device of the kettle type reaction device through a control circuit and an electromagnetic valve, so that the airtight reaction tank body of the kettle type reaction device achieves preset parameter conditions.\|[0020] In the preferred scheme of the invention, the control center of the building material carbonization test system is also provided with an integrated circuit chip and a touch screen; the touch screen can display a man-machine interaction interface, is used for displaying operation state parameters of the kettle type reaction device to an operator, and is used for inputting parameters and instructions by the operator; the integrated circuit chip utilizes an embedded program to complete data processing and control of each measurement and control unit and the touch screen.\|[0021] The carbonization test system of the building material has higher safety when being used for high-concentration carbonization test of the building material, the test result is more in accordance with the actual situation, the carbon absorption or carbon resistance of the building material under the condition of high-concentration carbon dioxide can be measured under normal pressure, and the carbon waste gas consumed by cement building materials, carbon fixation in deep environment, rock weathering or CO (carbon monoxide) can be consumed 2 The research of mineralization and the like has higher reference value.\|[0022] In a second aspect, the invention also provides a carbonization test system for building materials, which consumes carbon dioxide waste gas generated by cement factories or power plants, carbon sequestration in deep environments and rock weathering orCO 2 Mineralization and other research applications.\|[0023] In a preferred application of the invention, the building material carbonization test system is used for high-concentration carbonization test of building materials, and comprises the following steps: the building material test block is placed in an airtight reaction tank body of a kettle type reaction device of the building material carbonization test system, the airtight reaction tank body is vacuumized to negative pressure through a vacuumizing device of the kettle type reaction device, then carbon dioxide gas is rapidly filled into the airtight reaction tank body through a carbon dioxide gas input device of the kettle type reaction device, so that the air pressure in the airtight reaction tank body reaches normal pressure and the carbon dioxide concentration reaches more than 90%, then the temperature, the humidity and the air pressure in the airtight reaction tank body are regulated to reach preset values through a temperature regulating device, a humidity regulating device and an air pressure regulating device of the kettle type reaction device based on detection of a sensor group of the kettle type reaction device, and then the carbon absorption performance of the test block is observed according to a conventional method.\|[0024] In the preferred application of the invention, the application of the building material carbonization test system in consuming carbon dioxide waste gas generated by cement plants or power plants is to use the building material carbonization test system for carbon maintenance of building materials. The specific steps can be as follows: CO of cement kiln flue gas 2 After trapping, carbon dioxide is input into the airtight reaction tank body through the carbon dioxide input device of the building material carbonization test system, the building material is subjected to carbon curing, and the building material is subjected to constant pressure rapid reaction at the pressure of 1bar-15bar interval and normal temperature for 2 hours, so that the curing process is completed. Not only can greatly save maintenance cost, but also the building material can absorb CO 2 The post strength is obviously increased, and the obvious advantage of low carbon benefit can be reflected while the smoke is consumed.\|[0025] In the preferred application of the invention, the application of the building material carbonization test system in consuming carbon dioxide waste gas generated by cement plants or power plants is to use the building material carbonization test system in the study of durability of building materials. The carbonization test system for the building material can accelerate carbonization of a test piece of the building material by improving the temperature and the pressure of the test environment, thereby achieving the purpose of shortening the test period.\|[0026] In the application of the invention, the application of the building material carbonization test system in carbon sequestration in deep ground environment is that the building material carbonization test system is used as a test device for: (1) research on CO of inorganic building materials under high-temperature and high-pressure conditions 2 (2) researching influence of factors such as temperature, pressure and the like on carbonization rules, (3) researching CO under different stratum environments 2 Stable temperature and pressure relationship to promote the carbon sink technology, geological sealing technology or rock efflorescence and CO of inorganic building materials 2 Research on mineralization technology.\|[0027] In a preferred application of the invention, the building material carbonization test system is used for rock weathering or CO 2 The application in mineralization is to use the building material carbonization test system as a test device for simulating accelerated weathering and CO under high temperature and high pressure 2 Mineralization process for research of how to accelerate and enlarge CO 2 Is stable and stable.\|[0028] In the art, it is conventionally considered that the carbon dioxide absorption capacity of concrete needs to be tested in a high pressure state, but the inventors considered that from the principle that carbon dioxide enters and reacts in concrete, a more realistic carbon dioxide absorption capacity of concrete can be obtained by testing in high concentration carbon dioxide gas at normal pressure. On the one hand, the concrete is not easy to breathe, because the binding degree of the cementing material, sand and stones in the concrete is higher after hydration reaction, the higher the strength is, the stronger the inner compactness of the concrete is, and the through holes are hardly formed, so that the outside air is difficult to smoothly diffuse into the inside of the concrete. On the other hand, however, there are numerous blind holes in the concrete, in which air is present, which also acts as a barrier to the penetration of external gases into the interior. In the traditional high-concentration concrete carbonization test, the test condition is high pressure, air in the blind hole is not only not easy to discharge under the existence of external high pressure, but also can be compressed, so that the concentration of carbon dioxide in the blind hole of the concrete test block and the concentration of carbon dioxide outside the blind hole have great difference in the test process, and the external carbon dioxide is not easy to enter the blind hole and is fully absorbed. Although each blind hole has limited space, the overall impact on the carbon absorption capacity of the block will be significant when a large number of distributed blind holes in the block are not capable of sufficiently absorbing carbon dioxide.\|[0029] The testing method adopts the mode of vacuumizing firstly and filling the carbon dioxide later, and before filling the carbon dioxide, the gas in the blind hole in the concrete test block can be well discharged under the negative pressure state, a vacuum body is formed, the carbon dioxide can be easily sucked into the concrete test block after filling and can smoothly permeate into each corner and each hole in the concrete test block, and when the carbon dioxide is filled to reach normal pressure, the concentration of the carbon dioxide in the blind hole in the concrete is basically consistent with the concentration measured by an external sensor. This solves two problems: 1) Carbon dioxide can enter the concrete more easily after negative pressure is formed in the test block, and the absorption rate of the carbon dioxide can be rapidly measured, so that rapid evaluation is realized; 2) The potential safety hazard caused by positive pressure or high pressure can be reduced by testing under normal pressure, and the requirements on the bearing capacity and personnel qualification of laboratory equipment are greatly reduced. The carbonization test is generally carried out in a university or research institution, and if the carbonization test can meet the test requirement of high concentration under normal pressure, the test risk can be greatly reduced.\|[0030] Based on the same principle, the test method disclosed by the invention is also applicable to carbonization tests of other inorganic building materials with porous structures.\|DRAWINGS DESCRIPTION\|[0031] FIG. 1 is a schematic view showing the overall structure of the tank reactor according to example 1.\|[0032] FIGS. 2 and 3 are schematic views showing the overall internal structure of the tank reactor according to example 1, taken from different angles.\|[0033] FIG. 4 is a schematic view showing the overall structure of the carbonization test system for a building material according to example 2.\|INVENTION MODE\|Detailed Description\|[0034] In order that the above-recited objects, features and advantages of the present invention will become more apparent, a more particular description of the invention, briefly summarized below, may be had by way of example only, by reference to the appended drawings.\|[0035] In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, but the present invention may be practiced in other ways other than those described herein, and persons skilled in the art will readily appreciate that the present invention is not limited to the specific embodiments disclosed below.\|[0036] In the following detailed description of the embodiments of the present invention, reference is made to the accompanying drawings, which form a part hereof, and in which is shown by way of illustration only, the scope of the invention is not limited by the claims. In addition, the three-dimensional dimensions of length, width and depth should be included in actual fabrication.\|[0037] Example 1 building Material carbonization test kettle reactor\|A kettle type reaction device for carbonization test of building materials has an integral structure shown in figure 1 and comprises an airtight reaction tank body, wherein one end of a shell 100 of the airtight reaction tank body is provided with a sealing cover 101, and the other end of the shell is provided with a fan wind wheel 102. The top of the housing 100 is provided with a barometer 103, a thermometer 104, a hygrometer 105, an exhaust pipe 106, a carbon dioxide concentration sensor (not shown in the figure), and a safety valve 107. The housing 100 is provided with a carbon dioxide gas input pipe 108, an evacuation pipe 109, a water vapor input pipe 110, and an air or nitrogen gas input pipe 111 on the side. A drain 112 (not shown in fig. 1) is also provided at the bottom of the housing 100.\|[0038] As shown in fig. 2 and 3, the inner container 200 is further sleeved inside the outer shell 100 of the airtight reaction tank body, and a certain gap exists between the outer shell 100 and the inner container 200 and is fixedly connected through a plurality of through connectors 300. The inner container 200 is generally divided into a test block placing area and a gas mixing area, and a semi-closed partition board is arranged in the middle; the test block placing area is internally provided with a test block frame 201, and test blocks can be placed on the test block frame 201. The evacuating tube 109 arranged on the outer shell 100 penetrates into the inner container 200 and is opened in the test block placing area, and the pressure gauge 103, the temperature gauge 104 and the humidity gauge 105 arranged on the outer shell 100 are respectively connected with the pressure sensor, the temperature sensor 203 and the humidity sensor 204 arranged in the test block placing area in the inner container 200. A heating rod 205, a fan cover 206 and a plate heat exchanger 207 are arranged in the gas mixing zone. The carbon dioxide gas input pipe 108, the water vapor input pipe 110, the air input pipe 111, and the liquid discharge pipe 112 provided on the housing 100 are all inserted into the inner container 200 and opened in the gas mixing region.\|[0039] The pressure sensor, the temperature sensor 203 and the humidity sensor 204 are used for directly contacting the gas inside the liner 200; the carbon dioxide concentration sensor can be arranged inside or outside the airtight reaction tank body according to the requirement, and when the temperature of the gas inside the airtight reaction tank body is lower than 50 ℃, the carbon dioxide concentration sensor can be arranged inside and used for directly contacting the gas inside the liner 200; when the temperature of the gas in the airtight reaction tank body is greater than or equal to 50 ℃, the carbon dioxide concentration sensor is arranged outside the airtight reaction tank body and is used for contacting the gas which is collected from the airtight reaction tank body and then subjected to cooling and decompression.\|[0040] When the kettle type reaction device is used for carbonization reaction of building materials, the airtight reaction tank body formed by the shell 100, the sealing cover 101 and the liner 200 can provide an airtight space for accommodating test blocks and keep preset carbon dioxide concentration, temperature, air pressure and humidity environments; the heating rod 205, the fan wind wheel 102 and the plate heat exchanger 207 can be used as temperature adjusting devices for adjusting the temperature of the gas in the inner container 200 of the airtight reaction tank body; in addition, the fan wind wheel 102 can also be used for uniformly mixing the gas in the liner 200 to promote the circulation of the gas in the liner 200; the water vapor input pipe 110, the fan wind wheel 102 and the plate heat exchanger 207 are used as humidity adjusting devices for adjusting the humidity of the gas in the inner container 200 of the airtight reaction tank body; the vacuumizing tube 109, the exhaust tube 106 and the air (or nitrogen) input tube 111 together form an air pressure adjusting device which can be used for adjusting the pressure of the air in the inner container 200 of the airtight reaction tank body; the barometer 103, the thermometer 104, the hygrometer 105 and the carbon dioxide concentration meter form a sensor group together with a pressure sensor, a temperature sensor 203, a humidity sensor 204 and a carbon dioxide concentration sensor which are respectively connected with the barometer 103, the thermometer 104, the hygrometer 105 and the carbon dioxide concentration meter, and the sensor group is used for monitoring the air pressure, the temperature, the humidity and the carbon dioxide concentration in the liner 200; the carbon dioxide gas input pipe 108 is used for externally connecting carbon dioxide storage equipment, and inputting carbon dioxide gas into the inner container 200 of the airtight reaction tank body so as to reach the preset carbon dioxide gas concentration; the drain pipe 112 is used to drain the liquid accumulated at the bottom of the liner 200.\|[0041] Example 2 carbonization test System for building Material\|A carbonization test system for building materials has an overall structure shown in FIG. 4, and comprises a kettle-type reaction device and a control center as described in example 1; the control center is provided with a control cabinet 400, a control circuit board is arranged in the control cabinet 400, and a temperature measurement and control module, a humidity measurement and control module, a pressure measurement and control module, a carbon dioxide concentration measurement and control module, a control circuit and a chip are arranged on the control circuit board. The touch screen 401 capable of performing man-machine interaction is arranged outside the control cabinet 400. Each measurement and control module is electrically connected with a corresponding sensor of the kettle-type reaction device through an electric wire and an electromagnetic valve respectively, receives signals or data from the corresponding sensor, and controls the operation of a fan wind wheel 102, a water vapor input pipe 110, a heating rod 205, a plate heat exchanger 207, a vacuumizing pipe 109, an exhaust pipe 106, an air (or nitrogen) input pipe 111 and a carbon dioxide gas input pipe 108 of the kettle-type reaction device through a control circuit and the electromagnetic valve, so that the airtight reaction tank body of the kettle-type reaction device achieves preset parameter conditions. The touch screen 401 may display a man-machine interaction interface for displaying operation state parameters of the tank reactor to an operator, and for inputting parameters and instructions by the operator; the chip utilizes the embedded program to complete data processing and control of each measurement and control module and the touch screen.\|[0042] The building material carbonization test system of the embodiment has higher safety when being used for high-concentration carbonization test of building materials, the test result is more in accordance with the actual situation, the carbon absorption or carbon resistance of the building materials under the condition of high-concentration carbon dioxide can be measured under normal pressure, and the carbon waste gas generated by cement factories or power plants, carbon fixation of deep environments and rock weathering or CO are consumed 2 The research of mineralization and the like has higher reference value.\|[0043] Example 3 high concentration carbonization test method for building Material\|A high-concentration carbonization testing method for building materials adopts the system of the embodiment 2 of the invention, and comprises the following steps:\|the prepared test blocks of the building material are intensively placed on the test block holder 201 in the liner 200, and then the sealing cover 101 is closed and locked, so that an airtight space is formed inside the liner 200. Before testing, the inside of the inner container 200 of the airtight reaction tank body is vacuumized to negative pressure through the vacuumizing tube 109 of the kettle type reaction device, then the carbon dioxide gas is rapidly filled into the inner container 200 through the carbon dioxide gas input tube 108 on the airtight reaction tank body, so that the air pressure in the inner container 200 of the airtight reaction tank body reaches normal pressure and the carbon dioxide concentration reaches more than 90%, then based on the detection of the pressure sensor, the temperature sensor 203, the humidity sensor 204 and the carbon dioxide concentration sensor, the control center controls the operation of the fan wind wheel 102, the water vapor input tube 110, the heating rod 205, the plate heat exchanger 207, the vacuumizing tube 109, the exhaust tube 106, the air input tube 111 and the carbon dioxide gas input tube 108 according to the embedded programs and algorithms of the chips, so that the temperature, the humidity and the air pressure in the airtight reaction tank body reach preset values, and then the carbon absorption performance of the building material test block is observed according to the conventional method.	(CN116808978)\|TECHNICAL FIELD\|[0001] The invention relates to a kettle type reaction device capable of providing high-concentration carbon dioxide, which uses carbon dioxide waste gas to carry out inorganic building material maintenance, carbon sequestration in deep environment, rock weathering and CO 2 Mineralization and other research applications.\|BACKGROUND ART\|[0002] "Green" low carbonThe research and development of cement production technology, namely low-carbon/ultra-low-carbon concrete in the field of building materials, is a hot spot of research and development at the present stage. Meanwhile, in view of the fact that the carbon dioxide is absorbed and utilized by the concrete after being captured, the strength of the concrete can be greatly improved, so that how to achieve carbon neutralization and improve the strength of building materials in the building material industry is a new hot spot for research in the industry. Furthermore, for technical grade CO 2 The carbon collection and deep-ground carbon sequestration technology is also of great significance for realizing 'double carbon targets', wherein factors such as deep-ground environment temperature, pressure and the like influence carbonization rules and CO in different stratum environments 2 The problems of stability, temperature, pressure and the like are worthy of intensive research.\|[0003] In the development of "carbon-neutral" production technology and deep-ground carbon sequestration technology for building materials, in particular inorganic building materials, research into carbonization of concrete has been involved. The carbonization of concrete means that carbon dioxide in air and calcium hydroxide in cement stone are subjected to chemical action under the condition of existence of water to generate calcium carbonate and water. The carbonization process is a process that carbon dioxide gradually diffuses from the surface to the inside of the concrete. The most important effect of carbonization on concrete is: the early strength and the later strength of the concrete are improved rapidly, the deeper the carbonization depth is, the higher the strength of the concrete is, and the different carbon dioxide absorption capacities of different mixing ratios of the concrete can be embodied through the carbonization process. In order to match with the consumption of carbon dioxide waste gas, the CO of the concrete under the high-temperature and high-pressure conditions in the research and development of being absorbed by the concrete and the geological storage technology 2 The carbon absorption and carbon resistance of the concrete are required to be detected through a carbonization test.\|[0004] The alkaline component in the concrete material can be mixed with CO with the concentration of 0.04% in the atmosphere under the natural condition 2 The chemical reaction is carried out but the process is very slow, with the depth of carbonation generally "no more than" 10 mm over its life cycle. But can quickly realize concrete carbonization by the technical measures of concentration improvement, temperature rise, pressurization and the like, and the strength of the product is higher. In the prior art, the carbonization test process of concrete generally comprises the steps of delivering carbon dioxide-containing gas with a certain concentrationAnd (3) placing the sample into a closed container for holding the concrete test block, and observing the depth of carbon dioxide absorbed by the test block or permeated and diffused into the test block within a certain time. For the study of carbon dioxide absorption of concrete, the carbonization test for measuring carbon absorption performance thereof requires the use of high concentration carbon dioxide gas. In the current practice, a high-concentration high-pressure high-temperature carbonization box is used for concrete carbonization test, high-concentration carbon dioxide is pressed into concrete by using the pressure of high-pressure gas, and the absorption and neutralization effects of the concrete on the carbon dioxide are observed. The high pressure of the gas in this test is usually generated by charging a large amount of carbon dioxide gas into a closed container containing air in order to achieve a sufficiently high carbon dioxide concentration, and the gas is also used by the test person as a driving force for absorbing carbon dioxide in concrete. However, such high pressure tests not only require a high pressure resistant container, but also have special requirements for the skill qualification of the operators, which would otherwise present a significant production safety risk.\|DISCLOSURE\|Disclosure of Invention\|[0005] In view of the above technical background, a primary object of the present invention is: the kettle type reaction device for the carbonization test of the building material can provide a high-concentration carbon dioxide environment and has higher safety.\|[0006] A further object of the invention is: provides the kettle type reaction device for consuming carbon dioxide waste gas generated by cement plants or power plants, carbon solid storage in deep environment, rock efflorescence and CO by cement building materials 2 Mineralization and other research applications.\|[0007] The above object of the present invention is achieved by the following means:\|in a first aspect, the present invention provides a tank reactor for carbonization testing of building materials, comprising:\|the airtight reaction tank body is used as an airtight space for accommodating a test block and forming a preset environment of carbon dioxide concentration, temperature, air pressure and humidity;\|the temperature adjusting device is arranged in the airtight reaction tank body and used for adjusting the temperature in the airtight reaction tank body;\|the humidity adjusting device is used for adjusting the humidity in the airtight reaction tank body;\|the air pressure adjusting device is arranged on the airtight reaction tank body and is used for adjusting the air pressure in the airtight reaction tank body;\|the carbon dioxide gas input device is used for externally connecting carbon dioxide storage equipment and inputting carbon dioxide gas into the airtight reaction tank body;\|and the sensor group is used for monitoring the concentration, temperature, air pressure and humidity of the carbon dioxide in the airtight reaction tank body.\|[0008] In the tank reactor according to the present invention, the size, shape and material of the airtight reaction tank are not particularly limited, but it is necessary to have airtightness to maintain the pressure and concentration of the internal gas and to have a certain strength to avoid deformation due to the pressure difference between the inside and outside thereof.\|[0009] In the kettle-type reaction device, the temperature adjusting device consists of a heating device and a refrigerating device; the heating device can be a heating rod and the like; the refrigeration device may be an evaporator or the like.\|[0010] In the kettle-type reaction device, the humidity adjusting device is a water vapor input device arranged on the airtight reaction tank body, and water vapor is input into the airtight reaction tank body through an external water vapor generating device to increase the humidity.\|[0011] In the kettle-type reaction device, the air pressure adjusting device at least comprises a vacuumizing device. In a further preferred scheme, the air pressure adjusting device can further comprise an external air compressor, a nitrogen input device with pressure and the like.\|[0012] In the tank reactor according to a further preferred aspect of the present invention, a blower device is provided in the airtight reaction tank to promote circulation of the gas in the airtight reaction tank in order to uniformly mix the gas in the airtight reaction tank.\|[0013] In the kettle-type reaction device, the sensor group comprises a carbon dioxide concentration sensor, a temperature sensor, a pressure sensor and a humidity sensor. The temperature sensor, the pressure sensor and the humidity sensor are arranged on the airtight reaction tank body and are used for directly contacting the gas in the airtight reaction tank body; the carbon dioxide concentration sensor is arranged inside or outside the airtight reaction tank body, the carbon dioxide concentration sensor arranged inside the airtight reaction tank body is used for directly contacting the gas with the temperature lower than 50 ℃ in the airtight reaction tank body, and the carbon dioxide concentration sensor arranged outside the airtight reaction tank body is used for contacting the gas which is collected from the airtight reaction tank body and is subjected to cooling and decompression after the gas with the temperature higher than 50 ℃ is collected.\|[0014] In a preferred embodiment of the present invention, the inner space of the airtight reaction tank is divided into two communicating areas: the test block placing area and the gas mixing area; the test block placing area is used for intensively placing one or more than two test blocks, the sensor group is directly contacted with the gas of the test block placing area, and the vacuumizing device is used for vacuumizing the gas of the test block placing area; the gas mixing area is used for receiving water vapor and carbon dioxide gas from the outside of the airtight reaction tank body and heating the gas, the temperature adjusting device is arranged in the gas mixing area, and the water vapor input device and the carbon dioxide gas input device are both opened in the gas mixing area.\|[0015] In a preferred embodiment of the present invention, in order to better reduce heat dissipation by conduction from the inside of the airtight reaction tank to the outside, the airtight reaction tank is composed of an inner tank and an outer tank, the inner tank is nested in the outer tank, and a gap is left between the inner tank and the outer tank. In a more preferable scheme, the inner tank body and the outer tank body are fixedly connected through a plurality of devices which are mutually connected in a screwed mode.\|[0016] In a further preferred scheme of the invention, in order to more flexibly adjust the air pressure and the carbon dioxide concentration in the airtight reaction tank body, the airtight reaction tank body is also provided with a nitrogen or air input device; in a more preferred embodiment, the nitrogen or air inlet means is open to the gas mixing zone.\|[0017] In a further preferred scheme of the invention, the airtight reaction tank body is also provided with an exhaust device and a liquid discharge device which are used for discharging gas and liquid in the airtight reaction tank body.\|[0018] In a further preferred scheme of the invention, the airtight reaction tank body is also provided with a safety valve.\|[0019] On the basis, the invention also provides a carbonization test system for building materials, which comprises the kettle-type reaction device and a control center; the control center is provided with a temperature measurement and control unit, a humidity measurement and control unit, a pressure measurement and control unit and a carbon dioxide concentration measurement and control unit, wherein each measurement and control unit respectively receives signals or data from the temperature sensor, the humidity sensor, the pressure sensor and the carbon dioxide concentration sensor, and controls the operation of the temperature adjusting device, the humidity adjusting device, the air pressure adjusting device, the carbon dioxide input device and the fan device of the kettle type reaction device through a control circuit and an electromagnetic valve, so that the airtight reaction tank body of the kettle type reaction device achieves preset parameter conditions.\|[0020] In the preferred scheme of the invention, the control center of the building material carbonization test system is also provided with an integrated circuit chip and a touch screen; the touch screen can display a man-machine interaction interface, is used for displaying operation state parameters of the kettle type reaction device to an operator, and is used for inputting parameters and instructions by the operator; the integrated circuit chip utilizes an embedded program to complete data processing and control of each measurement and control unit and the touch screen.\|[0021] The carbonization test system of the building material has higher safety when being used for high-concentration carbonization test of the building material, the test result is more in accordance with the actual situation, the carbon absorption or carbon resistance of the building material under the condition of high-concentration carbon dioxide can be measured under normal pressure, and the carbon waste gas consumed by cement building materials, carbon fixation in deep environment, rock weathering or CO (carbon monoxide) can be consumed 2 The research of mineralization and the like has higher reference value.\|[0022] In a second aspect, the invention also provides a carbonization test system for building materials, which consumes carbon dioxide waste gas generated by cement factories or power plants, carbon sequestration in deep environments and rock weathering orCO 2 Mineralization and other research applications.\|[0023] In a preferred application of the invention, the building material carbonization test system is used for high-concentration carbonization test of building materials, and comprises the following steps: the building material test block is placed in an airtight reaction tank body of a kettle type reaction device of the building material carbonization test system, the airtight reaction tank body is vacuumized to negative pressure through a vacuumizing device of the kettle type reaction device, then carbon dioxide gas is rapidly filled into the airtight reaction tank body through a carbon dioxide gas input device of the kettle type reaction device, so that the air pressure in the airtight reaction tank body reaches normal pressure and the carbon dioxide concentration reaches more than 90%, then the temperature, the humidity and the air pressure in the airtight reaction tank body are regulated to reach preset values through a temperature regulating device, a humidity regulating device and an air pressure regulating device of the kettle type reaction device based on detection of a sensor group of the kettle type reaction device, and then the carbon absorption performance of the test block is observed according to a conventional method.\|[0024] In the preferred application of the invention, the application of the building material carbonization test system in consuming carbon dioxide waste gas generated by cement plants or power plants is to use the building material carbonization test system for carbon maintenance of building materials. The specific steps can be as follows: CO of cement kiln flue gas 2 After trapping, carbon dioxide is input into the airtight reaction tank body through the carbon dioxide input device of the building material carbonization test system, the building material is subjected to carbon curing, and the building material is subjected to constant pressure rapid reaction at the pressure of 1bar-15bar interval and normal temperature for 2 hours, so that the curing process is completed. Not only can greatly save maintenance cost, but also the building material can absorb CO 2 The post strength is obviously increased, and the obvious advantage of low carbon benefit can be reflected while the smoke is consumed.\|[0025] In the preferred application of the invention, the application of the building material carbonization test system in consuming carbon dioxide waste gas generated by cement plants or power plants is to use the building material carbonization test system in the study of durability of building materials. The carbonization test system for the building material can accelerate carbonization of a test piece of the building material by improving the temperature and the pressure of the test environment, thereby achieving the purpose of shortening the test period.\|[0026] In the application of the invention, the application of the building material carbonization test system in carbon sequestration in deep ground environment is that the building material carbonization test system is used as a test device for: (1) research on CO of inorganic building materials under high-temperature and high-pressure conditions 2 (2) researching influence of factors such as temperature, pressure and the like on carbonization rules, (3) researching CO under different stratum environments 2 Stable temperature and pressure relationship to promote the carbon sink technology, geological sealing technology or rock efflorescence and CO of inorganic building materials 2 Research on mineralization technology.\|[0027] In a preferred application of the invention, the building material carbonization test system is used for rock weathering or CO 2 The application in mineralization is to use the building material carbonization test system as a test device for simulating accelerated weathering and CO under high temperature and high pressure 2 Mineralization process for research of how to accelerate and enlarge CO 2 Is stable and stable.\|[0028] In the art, it is conventionally considered that the carbon dioxide absorption capacity of concrete needs to be tested in a high pressure state, but the inventors considered that from the principle that carbon dioxide enters and reacts in concrete, a more realistic carbon dioxide absorption capacity of concrete can be obtained by testing in high concentration carbon dioxide gas at normal pressure. On the one hand, the concrete is not easy to breathe, because the binding degree of the cementing material, sand and stones in the concrete is higher after hydration reaction, the higher the strength is, the stronger the inner compactness of the concrete is, and the through holes are hardly formed, so that the outside air is difficult to smoothly diffuse into the inside of the concrete. On the other hand, however, there are numerous blind holes in the concrete, in which air is present, which also acts as a barrier to the penetration of external gases into the interior. In the traditional high-concentration concrete carbonization test, the test condition is high pressure, air in the blind hole is not only not easy to discharge under the existence of external high pressure, but also can be compressed, so that the concentration of carbon dioxide in the blind hole of the concrete test block and the concentration of carbon dioxide outside the blind hole have great difference in the test process, and the external carbon dioxide is not easy to enter the blind hole and is fully absorbed. Although each blind hole has limited space, the overall impact on the carbon absorption capacity of the block will be significant when a large number of distributed blind holes in the block are not capable of sufficiently absorbing carbon dioxide.\|[0029] The testing method adopts the mode of vacuumizing firstly and filling the carbon dioxide later, and before filling the carbon dioxide, the gas in the blind hole in the concrete test block can be well discharged under the negative pressure state, a vacuum body is formed, the carbon dioxide can be easily sucked into the concrete test block after filling and can smoothly permeate into each corner and each hole in the concrete test block, and when the carbon dioxide is filled to reach normal pressure, the concentration of the carbon dioxide in the blind hole in the concrete is basically consistent with the concentration measured by an external sensor. This solves two problems: 1) Carbon dioxide can enter the concrete more easily after negative pressure is formed in the test block, and the absorption rate of the carbon dioxide can be rapidly measured, so that rapid evaluation is realized; 2) The potential safety hazard caused by positive pressure or high pressure can be reduced by testing under normal pressure, and the requirements on the bearing capacity and personnel qualification of laboratory equipment are greatly reduced. The carbonization test is generally carried out in a university or research institution, and if the carbonization test can meet the test requirement of high concentration under normal pressure, the test risk can be greatly reduced.\|[0030] Based on the same principle, the test method disclosed by the invention is also applicable to carbonization tests of other inorganic building materials with porous structures.\|DRAWINGS DESCRIPTION\|[0031] FIG. 1 is a schematic view showing the overall structure of the tank reactor according to example 1.\|[0032] FIGS. 2 and 3 are schematic views showing the overall internal structure of the tank reactor according to example 1, taken from different angles.\|[0033] FIG. 4 is a schematic view showing the overall structure of the carbonization test system for a building material according to example 2.\|INVENTION MODE\|Detailed Description\|[0034] In order that the above-recited objects, features and advantages of the present invention will become more apparent, a more particular description of the invention, briefly summarized below, may be had by way of example only, by reference to the appended drawings.\|[0035] In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, but the present invention may be practiced in other ways other than those described herein, and persons skilled in the art will readily appreciate that the present invention is not limited to the specific embodiments disclosed below.\|[0036] In the following detailed description of the embodiments of the present invention, reference is made to the accompanying drawings, which form a part hereof, and in which is shown by way of illustration only, the scope of the invention is not limited by the claims. In addition, the three-dimensional dimensions of length, width and depth should be included in actual fabrication.\|[0037] Example 1 building Material carbonization test kettle reactor\|A kettle type reaction device for carbonization test of building materials has an integral structure shown in figure 1 and comprises an airtight reaction tank body, wherein one end of a shell 100 of the airtight reaction tank body is provided with a sealing cover 101, and the other end of the shell is provided with a fan wind wheel 102. The top of the housing 100 is provided with a barometer 103, a thermometer 104, a hygrometer 105, an exhaust pipe 106, a carbon dioxide concentration sensor (not shown in the figure), and a safety valve 107. The housing 100 is provided with a carbon dioxide gas input pipe 108, an evacuation pipe 109, a water vapor input pipe 110, and an air or nitrogen gas input pipe 111 on the side. A drain 112 (not shown in fig. 1) is also provided at the bottom of the housing 100.\|[0038] As shown in fig. 2 and 3, the inner container 200 is further sleeved inside the outer shell 100 of the airtight reaction tank body, and a certain gap exists between the outer shell 100 and the inner container 200 and is fixedly connected through a plurality of through connectors 300. The inner container 200 is generally divided into a test block placing area and a gas mixing area, and a semi-closed partition board is arranged in the middle; the test block placing area is internally provided with a test block frame 201, and test blocks can be placed on the test block frame 201. The evacuating tube 109 arranged on the outer shell 100 penetrates into the inner container 200 and is opened in the test block placing area, and the pressure gauge 103, the temperature gauge 104 and the humidity gauge 105 arranged on the outer shell 100 are respectively connected with the pressure sensor, the temperature sensor 203 and the humidity sensor 204 arranged in the test block placing area in the inner container 200. A heating rod 205, a fan cover 206 and a plate heat exchanger 207 are arranged in the gas mixing zone. The carbon dioxide gas input pipe 108, the water vapor input pipe 110, the air input pipe 111, and the liquid discharge pipe 112 provided on the housing 100 are all inserted into the inner container 200 and opened in the gas mixing region.\|[0039] The pressure sensor, the temperature sensor 203 and the humidity sensor 204 are used for directly contacting the gas inside the liner 200; the carbon dioxide concentration sensor can be arranged inside or outside the airtight reaction tank body according to the requirement, and when the temperature of the gas inside the airtight reaction tank body is lower than 50 ℃, the carbon dioxide concentration sensor can be arranged inside and used for directly contacting the gas inside the liner 200; when the temperature of the gas in the airtight reaction tank body is greater than or equal to 50 ℃, the carbon dioxide concentration sensor is arranged outside the airtight reaction tank body and is used for contacting the gas which is collected from the airtight reaction tank body and then subjected to cooling and decompression.\|[0040] When the kettle type reaction device is used for carbonization reaction of building materials, the airtight reaction tank body formed by the shell 100, the sealing cover 101 and the liner 200 can provide an airtight space for accommodating test blocks and keep preset carbon dioxide concentration, temperature, air pressure and humidity environments; the heating rod 205, the fan wind wheel 102 and the plate heat exchanger 207 can be used as temperature adjusting devices for adjusting the temperature of the gas in the inner container 200 of the airtight reaction tank body; in addition, the fan wind wheel 102 can also be used for uniformly mixing the gas in the liner 200 to promote the circulation of the gas in the liner 200; the water vapor input pipe 110, the fan wind wheel 102 and the plate heat exchanger 207 are used as humidity adjusting devices for adjusting the humidity of the gas in the inner container 200 of the airtight reaction tank body; the vacuumizing tube 109, the exhaust tube 106 and the air (or nitrogen) input tube 111 together form an air pressure adjusting device which can be used for adjusting the pressure of the air in the inner container 200 of the airtight reaction tank body; the barometer 103, the thermometer 104, the hygrometer 105 and the carbon dioxide concentration meter form a sensor group together with a pressure sensor, a temperature sensor 203, a humidity sensor 204 and a carbon dioxide concentration sensor which are respectively connected with the barometer 103, the thermometer 104, the hygrometer 105 and the carbon dioxide concentration meter, and the sensor group is used for monitoring the air pressure, the temperature, the humidity and the carbon dioxide concentration in the liner 200; the carbon dioxide gas input pipe 108 is used for externally connecting carbon dioxide storage equipment, and inputting carbon dioxide gas into the inner container 200 of the airtight reaction tank body so as to reach the preset carbon dioxide gas concentration; the drain pipe 112 is used to drain the liquid accumulated at the bottom of the liner 200.\|[0041] Example 2 carbonization test System for building Material\|A carbonization test system for building materials has an overall structure shown in FIG. 4, and comprises a kettle-type reaction device and a control center as described in example 1; the control center is provided with a control cabinet 400, a control circuit board is arranged in the control cabinet 400, and a temperature measurement and control module, a humidity measurement and control module, a pressure measurement and control module, a carbon dioxide concentration measurement and control module, a control circuit and a chip are arranged on the control circuit board. The touch screen 401 capable of performing man-machine interaction is arranged outside the control cabinet 400. Each measurement and control module is electrically connected with a corresponding sensor of the kettle-type reaction device through an electric wire and an electromagnetic valve respectively, receives signals or data from the corresponding sensor, and controls the operation of a fan wind wheel 102, a water vapor input pipe 110, a heating rod 205, a plate heat exchanger 207, a vacuumizing pipe 109, an exhaust pipe 106, an air (or nitrogen) input pipe 111 and a carbon dioxide gas input pipe 108 of the kettle-type reaction device through a control circuit and the electromagnetic valve, so that the airtight reaction tank body of the kettle-type reaction device achieves preset parameter conditions. The touch screen 401 may display a man-machine interaction interface for displaying operation state parameters of the tank reactor to an operator, and for inputting parameters and instructions by the operator; the chip utilizes the embedded program to complete data processing and control of each measurement and control module and the touch screen.\|[0042] The building material carbonization test system of the embodiment has higher safety when being used for high-concentration carbonization test of building materials, the test result is more in accordance with the actual situation, the carbon absorption or carbon resistance of the building materials under the condition of high-concentration carbon dioxide can be measured under normal pressure, and the carbon waste gas generated by cement factories or power plants, carbon fixation of deep environments and rock weathering or CO are consumed 2 The research of mineralization and the like has higher reference value.\|[0043] Example 3 high concentration carbonization test method for building Material\|A high-concentration carbonization testing method for building materials adopts the system of the embodiment 2 of the invention, and comprises the following steps:\|the prepared test blocks of the building material are intensively placed on the test block holder 201 in the liner 200, and then the sealing cover 101 is closed and locked, so that an airtight space is formed inside the liner 200. Before testing, the inside of the inner container 200 of the airtight reaction tank body is vacuumized to negative pressure through the vacuumizing tube 109 of the kettle type reaction device, then the carbon dioxide gas is rapidly filled into the inner container 200 through the carbon dioxide gas input tube 108 on the airtight reaction tank body, so that the air pressure in the inner container 200 of the airtight reaction tank body reaches normal pressure and the carbon dioxide concentration reaches more than 90%, then based on the detection of the pressure sensor, the temperature sensor 203, the humidity sensor 204 and the carbon dioxide concentration sensor, the control center controls the operation of the fan wind wheel 102, the water vapor input tube 110, the heating rod 205, the plate heat exchanger 207, the vacuumizing tube 109, the exhaust tube 106, the air input tube 111 and the carbon dioxide gas input tube 108 according to the embedded programs and algorithms of the chips, so that the temperature, the humidity and the air pressure in the airtight reaction tank body reach preset values, and then the carbon absorption performance of the building material test block is observed according to the conventional method.	Family Number\|(106692037)\|106692037\|Object of Invention\|(CN116808978 A)\|( . . . ) The invention also provides the building material carbonization test system for carbon sequestration and rock weathering or CO in the deep environment consuming carbon dioxide waste gas 2 Mineralization and other research applications . \|The invention relates to a kettle type reaction device capable of providing high - concentration carbon dioxide , which uses carbon dioxide waste gas to carry out inorganic building material maintenance , carbon sequestration in deep environment , rock weathering and CO 2 Mineralization and other research applications . \|Abstract\|(CN116808978 A)\|The invention provides a kettle type reaction device for a carbonization test of a building material . The kettle type reaction device comprises an airtight reaction tank body , a temperature adjusting device , a humidity adjusting device , an air pressure adjusting device , a carbon dioxide gas input device and a sensor group . The invention further provides a building material carbonization test system . The building material carbonization test system comprises the kettle type reaction device and a control center . The invention also provides an application of the building material carbonization test system in researches such as consumption of carbon dioxide waste gas , carbon immobilization in a deep ground environment , rock weathering or CO2 mineralization and the like . The building material carbonization test system disclosed by the invention has higher safety when being used for high - concentration carbonization test of the building material , the test result is more in line with the real situation , and the carbon absorption or carbon resistance of the building material under the condition of high - concentration carbon dioxide can be measured under normal pressure ; the method has higher reference value for research on consumption of carbon dioxide waste gas , carbon immobilization of deep ground environment , rock weathering or CO2 mineralization and the like . \|	Analysis of biological materials\|Chemical engineering\|Other special machines				B01J-019/00\|B01J-019/24\|B28B-011/24\|G01D-021/02\|G01N-033/38	B01J-019/00\|B01J-019/24\|B28B-011/24\|G01D-021/02\|G01N-033/38					CN219092083U\|CN116252380\|CN219111536U\|CN217247947U\|CN206002540U\|KR100686495	CN219092083U 105134867 WHO=Examiner SELF=N CAT=Y CAT=X\|CN116252380 105291149 WHO=Examiner SELF=N CAT=Y\|CN219111536U 105174535 WHO=Examiner SELF=N CAT=A\|CN217247947U 101445038 WHO=Examiner SELF=N CAT=A\|CN206002540U 75611541 WHO=Examiner SELF=N CAT=A\|KR100686495 34004485 WHO=Examiner SELF=N CAT=A		KR100686495; CN219092083U; CN219111536U; CN116252380; CN206002540U; CN217247947U		REVOKED	(CN116808978)\|REVOKED	DEAD	(CN116808978)\|DEAD	(CN116808978)\|LEGAL DETAILS FOR CN116808978\|Actual or expected expiration date=2025-02-21\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2023-07-17\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202310871419\|Application date=2023-07-17\|Standardized application number=2023CN-0871419\|Event publication date=2023-09-29\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN116808978\|Publication stage code=A\|Publication date=2023-09-29\|Standardized publication number=CN116808978\|Event publication date=2023-09-29\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2023-10-24\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2025-02-21\|Event code=CN/RJ01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Rejection of an application after its publication			https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoS5zxZVvzcMc1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000069675907&ekey=2236&xpn=CN116808978&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=vv3VyocLermzgUb19TswmZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN116808978)\|CN	(CN116808978)\|NAME=NELD INTELLIGENT TECHNOLOGY XIANGHE CO., LTD. , COUNTRY=CN		(CN116808978)\|NAME=LIU JUNLING;BEIJING ZHAOJUN UNION INTELLECTUAL PROPERTY LAW FIRM , REG=11333		(CN116808978)\|NAME=ZHANG HUIYI	(CN116808978)\|3	1	1					(CN116808978)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2023-09-29\|Gazette number: GAZNUM=39-3902\|Number of Pages: NPAGES=13\|		(CN116808978)\|CHINESE (CHI)	(CN116808978)\|Patent	Titre: (CN116808978)\|Kettle-type reaction device for carbonization test of building materials and application of kettle-type reaction device Résumé: (CN116808978)\|The invention provides a kettle type reaction device for a carbonization test of a building material. The kettle type reaction device comprises an airtight reaction tank body, a temperature adjusting device, a humidity adjusting device, an air pressure adjusting device, a carbon dioxide gas input device and a sensor group. The invention further provides a building material carbonization test system. The building material carbonization test system comprises the kettle type reaction device and a control center. The invention also provides an application of the building material carbonization test system in researches such as consumption of carbon dioxide waste gas, carbon immobilization in a deep ground environment, rock weathering or CO2 mineralization and the like. The building material carbonization test system disclosed by the invention has higher safety when being used for high-concentration carbonization test of the building material, the test result is more in line with the real situation, and the carbon absorption or carbon resistance of the building material under the condition of high-concentration carbon dioxide can be measured under normal pressure; the method has higher reference value for research on consumption of carbon dioxide waste gas, carbon immobilization of deep ground environment, rock weathering or CO2 mineralization and the like.	23	Abstract	gpt-4o-mini	no	The focus is on carbonization tests of building materials, not on accelerated weathering or CO2 capture through mineral alteration.
24	US05/892,043\|US06/068,316	US06/068,316\|ZA791501\|DK128479\|IT4852779\|JPS54-35156\|EP79400191\|DE2962375T\|AU4533979\|CA322199	CA1124031\|DE2962375\|EP0004807\|AU520262\|US4299805\|ZA791501\|EP0004807\|EP0004807\|JPS54-133498\|AU4533979\|DK128479\|IT7948527	1081365	US4299805 A 1981-11-10 [US4299805]\|ZA791501 B 1980-11-26 [ZA7901501]\|DK128479 A 1979-10-01 [DK7901284]\|IT7948527 A0 1979-03-29 [IT7948527]\|JPS54-133498 A 1979-10-17 [JP54133498]\|EP0004807 B1 1982-03-31 [EP---4807]\|EP0004807 A3 1979-10-31 [EP---4807]\|EP0004807 A2 1979-10-17 [EP---4807]\|DE2962375 D1 1982-05-06 [DE2962375]\|AU520262 B2 1982-01-21 [AU-520262]\|AU4533979 A 1979-10-04 [AU7945339]\|CA1124031 A 1982-05-25 [CA1124031]	1978-03-30\|1979-08-21	1979-08-21\|1979-03-29\|1979-03-29\|1979-03-29\|1979-03-27\|1979-03-26\|1979-03-26\|1979-03-22\|1979-02-23	1982-05-25\|1982-05-06\|1982-03-31\|1982-01-21\|1981-11-10\|1980-11-26\|1979-10-31\|1979-10-17\|1979-10-17\|1979-10-04\|1979-10-01\|1979-03-29	(EP---4807)\|1982-03-31\|(US4299805)\|1981-11-10\|(DE2962375)\|1982-05-06\|\|(CA1124031)\|1982-05-25\|(AU-520262)\|1982-01-21\|(ZA7901501)\|1980-11-26\|\|	(EP0004807)\|1999-03-26\|(US4299805)\|1998-11-10\|(DE2962375)\|1986-12-02\|(JPS54-133498)\|1988-10-17\|(CA1124031)\|1999-05-25\|(AU520262)\|1998-01-21\|(ZA791501)\|1999-03-29\|(DK128479)\|1984-10-01\|(IT7948527)\|1999-03-29	(EP0004807)\|Regeneration of carbon employed in the wet process production of phosphoric acid	(EP0004807)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.	CALGON\|CALGON CARBON\|U	(EP0004807)\|CALGON CORPORATION ([US])\|(EP0004807)\|Calgon Corporation\|(EP0004807)\|CALGON CORPORATION ([US])\|(US4299805)\|Calgon Corporation ([US])\|(DE2962375)\|CALGON CORPORATION\|(JPS54-133498)\|CALGON CORP\|(CA1124031)\|CALGON CORPORATION ([US])\|(AU520262)\|CALGON CORPORATION\|(AU4533979)\|CALGON CORPORATION\|(ZA791501)\|CALGON CORP\|(DK128479)\|CALGON CORPORATION\|(IT7948527)\|CALGON CORPORATION\|U.S.A.	WELLS, BRUCE DOUGLAS\|TIGGELBECK, DONALD DAVID	(EP0004807)\|Wells, Bruce Douglas\|Tiggelbeck, Donald David\|(EP0004807)\|Wells, Bruce Douglas\|Tiggelbeck, Donald David\|(EP0004807)\|Wells, Bruce Douglas\|Tiggelbeck, Donald David	(EP0004807)\|Corre, Jacques Denis Paul;Cabinet Regimbeau ([FR])\|Reg. Nb: 00014911\|(US4299805)\|Katz Martin L.\|Riedl Edmunde D.\|Olson R. Brent\|(CA1124031)\|GOUDREAU, GAGE & ASSOCIATES ([CA])	(EP0004807)\|Generally, the so-called liquid phase activated carbons are preferred since their pore size distribution is sufficiently large to allow for easy access of liquids to the interior of the pores.\|Indeed, the exact nature of the contaminants is difficult to state with precision since the composition of the raw phosphate rock will differ with the run of the mine and even more widely from mine to mine.\|	(EP0004807)\|1. A process for regenerating activated carbon employed for removal of contamination from brown phosphoric acid or aqueous solution of crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by passing aqueous solution comprising 1% to 50% by weight of a base through said activated charcoal and subsequent thereto passing a 0.5 to 2.0N aqueous solution of mineral acid other than brown phosphoric acid through said activated carbon.\|2. In the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1-10 hours; washing the activated carbon with water to remove residual base; contacting the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1-16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|	(EP0004807)\|The present invention is also directed to the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1 to 10 hours; washing the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1 to 16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|This invention relates to an improved process for recycling and regenerating activated carbon employed in the purification of phosphoric acid produced by the wet-process.\|	(EP0004807)\|PHOSPHORIC ACID(100,41)\|BROWN PHOSPHORIC ACID(100,10)\|AQUEOUS SOLUTION(100,9)\|ACTIVATED CARBON REGENERATION(100,6)\|BROWN PHOSPHORIC ACID FILTRATION(100,4)\|ALKALI METAL RAW(100,3)\|CARBON REGENERATION(100,3)\|CRUDE ALKALI METAL PHOSPHATE 3(100,3)\|ALKALI PHOSPHATE 3(100,2)\|PRODUCING PHOSPHORIC ACID(100,2)\|CONTAMINATION REMOVAL(100,1)\|PRODUCING WET(100,1)\|ALKALI TREATMENT(72,3)\|BROWN RESIDUE(72,2)\|RESIDUAL BROWN PHOSPHORIC ACID(63,2)\|ACTIVATED CARBON(50,49)\|MINERAL ACID(41,10)\|PHOSPHORIC ACID PURIFICATION(37,1)\|SEQUENTIAL BATCH(37,1)\|ASH CONTENT(29,1)\|RECYCLING(29,1)\|RESIDUAL ALKALI(29,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(27,1)\|ACTIVATED CHARCOAL(22,2)\|PORE SIZE(20,2)\|ROCK(17,2)\|SODIUM HYDROXIDE(11,2)\|DIGESTION DEBACTEROL(11,1)\|GYPSUM GROSS PARTICLE(11,1)\|PHOSPHATIC FERTILIZER(11,1)\|PHOTOMETRY COLORIMETRY(11,1)\|LIQUID PHASE(9,1)\|LIQUID PHASE ACTIVATED CARBON(9,1)\|PULVERIZE ROCK(9,1)\|THRICE REPEATED DRAINING(9,1)\|ALKANOL AMMONIA(8,1)\|BROWN TINGE(8,1)\|CONTAMINANT VARIED MIX(8,1)\|NEUTRALIZE CRUDE(8,1)\|ROCK IMPURITY(8,1)\|UNDUE DETRIMENT(8,1)\|MARGINAL ARROW(6,1)\|NI TRICE(6,1)\|PETROLEUM ACID SLUDGE(6,1)\|RAW BROWN(6,1)\|TRICKLE BED(6,1)\|VIRGIN CAPACITY(6,1)\|BROWN ACID(5,2)\|GRADE PHOSPHORIC ACID(5,2)\|GREEN PHOSPHORIC ACID(5,2)\|REFILLING(5,2)\|ACTIVATED CARBON INTERMITTENT WASHING(5,1)\|ALKALI CARBONATE(5,1)\|BROWN PRODUCTION(5,1)\|CAUSTIC SOLUTION(5,1)\|COMPLEX SILICATE(5,1)\|ELECTROTHERMAL PHOSPHORIC ACID(5,1)\|ELEMINATED(5,1)\|FLUSHING(5,1)\|GRANULAR CARBON(5,1)\|PAST FOOD(5,1)\|RESIDUAL PHOSPHORIC ACID BULK(5,1)\|ACTIVATED CARBON BED(4,3)\|PATHWAY(4,2)\|ACIDIC WASH(4,1)\|ACTIVATED CARBON PURIFICATION(4,1)\|BACKWASH(4,1)\|BITUMINOUS COAL(4,1)\|CAPITAL INVESTMENT(4,1)\|COMPLETION(4,1)\|CRUSHING(4,1)\|DISPOSAL(4,1)\|EFFLUENT(4,1)\|ELEMENTAL PHOSPHORIC ACID(4,1)\|EXCESS SALT(4,1)\|EXPERIMENTATION(4,1)\|FOOD PRODUCTION(4,1)\|IMPURITE(4,1)\|INFLUX(4,1)\|LIGNITE(4,1)\|NEUTRALIZING(4,1)\|OCCASION(4,1)\|\|(EP0004807)\|PHOSPHORIC ACID(100,41)\|BROWN PHOSPHORIC ACID(100,10)\|AQUEOUS SOLUTION(100,9)\|ACTIVATED CARBON REGENERATION(100,6)\|BROWN PHOSPHORIC ACID FILTRATION(100,4)\|ALKALI METAL RAW(100,3)\|CARBON REGENERATION(100,3)\|CRUDE ALKALI METAL PHOSPHATE 3(100,3)\|ALKALI PHOSPHATE 3(100,2)\|PRODUCING PHOSPHORIC ACID(100,2)\|CONTAMINATION REMOVAL(100,1)\|PRODUCING WET(100,1)\|ALKALI TREATMENT(72,3)\|BROWN RESIDUE(72,2)\|RESIDUAL BROWN PHOSPHORIC ACID(63,2)\|ACTIVATED CARBON(50,49)\|MINERAL ACID(41,10)\|PHOSPHORIC ACID PURIFICATION(37,1)\|SEQUENTIAL BATCH(37,1)\|ASH CONTENT(29,1)\|RECYCLING(29,1)\|RESIDUAL ALKALI(29,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(27,1)\|ACTIVATED CHARCOAL(22,2)\|PORE SIZE(20,2)\|ROCK(17,2)\|SODIUM HYDROXIDE(11,2)\|DIGESTION DEBACTEROL(11,1)\|GYPSUM GROSS PARTICLE(11,1)\|PHOSPHATIC FERTILIZER(11,1)\|PHOTOMETRY COLORIMETRY(11,1)\|LIQUID PHASE(9,1)\|LIQUID PHASE ACTIVATED CARBON(9,1)\|PULVERIZE ROCK(9,1)\|THRICE REPEATED DRAINING(9,1)\|ALKANOL AMMONIA(8,1)\|BROWN TINGE(8,1)\|CONTAMINANT VARIED MIX(8,1)\|NEUTRALIZE CRUDE(8,1)\|ROCK IMPURITY(8,1)\|UNDUE DETRIMENT(8,1)\|MARGINAL ARROW(6,1)\|NI TRICE(6,1)\|PETROLEUM ACID SLUDGE(6,1)\|RAW BROWN(6,1)\|TRICKLE BED(6,1)\|VIRGIN CAPACITY(6,1)\|BROWN ACID(5,2)\|GRADE PHOSPHORIC ACID(5,2)\|GREEN PHOSPHORIC ACID(5,2)\|REFILLING(5,2)\|ACTIVATED CARBON INTERMITTENT WASHING(5,1)\|ALKALI CARBONATE(5,1)\|BROWN PRODUCTION(5,1)\|CAUSTIC SOLUTION(5,1)\|COMPLEX SILICATE(5,1)\|ELECTROTHERMAL PHOSPHORIC ACID(5,1)\|ELEMINATED(5,1)\|FLUSHING(5,1)\|GRANULAR CARBON(5,1)\|PAST FOOD(5,1)\|RESIDUAL PHOSPHORIC ACID BULK(5,1)\|ACTIVATED CARBON BED(4,3)\|PATHWAY(4,2)\|ACIDIC WASH(4,1)\|ACTIVATED CARBON PURIFICATION(4,1)\|BACKWASH(4,1)\|BITUMINOUS COAL(4,1)\|CAPITAL INVESTMENT(4,1)\|COMPLETION(4,1)\|CRUSHING(4,1)\|DISPOSAL(4,1)\|EFFLUENT(4,1)\|ELEMENTAL PHOSPHORIC ACID(4,1)\|EXCESS SALT(4,1)\|EXPERIMENTATION(4,1)\|FOOD PRODUCTION(4,1)\|IMPURITE(4,1)\|INFLUX(4,1)\|LIGNITE(4,1)\|NEUTRALIZING(4,1)\|OCCASION(4,1)\|\|(EP0004807)\|PHOSPHORIC ACID(100,41)\|BROWN PHOSPHORIC ACID(100,10)\|AQUEOUS SOLUTION(100,9)\|ACTIVATED CARBON REGENERATION(100,6)\|BROWN PHOSPHORIC ACID FILTRATION(100,4)\|ALKALI METAL RAW(100,3)\|CARBON REGENERATION(100,3)\|CRUDE ALKALI METAL PHOSPHATE 3(100,3)\|ALKALI PHOSPHATE 3(100,2)\|PRODUCING PHOSPHORIC ACID(100,2)\|CONTAMINATION REMOVAL(100,1)\|PRODUCING WET(100,1)\|ALKALI TREATMENT(72,3)\|BROWN RESIDUE(72,2)\|RESIDUAL BROWN PHOSPHORIC ACID(63,2)\|ACTIVATED CARBON(50,49)\|MINERAL ACID(41,10)\|PHOSPHORIC ACID PURIFICATION(37,1)\|SEQUENTIAL BATCH(37,1)\|ASH CONTENT(29,1)\|RECYCLING(29,1)\|RESIDUAL ALKALI(29,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(27,1)\|ACTIVATED CHARCOAL(22,2)\|PORE SIZE(20,2)\|ROCK(17,2)\|SODIUM HYDROXIDE(11,2)\|DIGESTION DEBACTEROL(11,1)\|GYPSUM GROSS PARTICLE(11,1)\|PHOSPHATIC FERTILIZER(11,1)\|PHOTOMETRY COLORIMETRY(11,1)\|LIQUID PHASE(9,1)\|LIQUID PHASE ACTIVATED CARBON(9,1)\|PULVERIZE ROCK(9,1)\|THRICE REPEATED DRAINING(9,1)\|ALKANOL AMMONIA(8,1)\|BROWN TINGE(8,1)\|CONTAMINANT VARIED MIX(8,1)\|NEUTRALIZE CRUDE(8,1)\|ROCK IMPURITY(8,1)\|UNDUE DETRIMENT(8,1)\|MARGINAL ARROW(6,1)\|NI TRICE(6,1)\|PETROLEUM ACID SLUDGE(6,1)\|RAW BROWN(6,1)\|TRICKLE BED(6,1)\|VIRGIN CAPACITY(6,1)\|BROWN ACID(5,2)\|GRADE PHOSPHORIC ACID(5,2)\|GREEN PHOSPHORIC ACID(5,2)\|REFILLING(5,2)\|ACTIVATED CARBON INTERMITTENT WASHING(5,1)\|ALKALI CARBONATE(5,1)\|BROWN PRODUCTION(5,1)\|CAUSTIC SOLUTION(5,1)\|COMPLEX SILICATE(5,1)\|ELECTROTHERMAL PHOSPHORIC ACID(5,1)\|ELEMINATED(5,1)\|FLUSHING(5,1)\|GRANULAR CARBON(5,1)\|PAST FOOD(5,1)\|RESIDUAL PHOSPHORIC ACID BULK(5,1)\|ACTIVATED CARBON BED(4,3)\|PATHWAY(4,2)\|ACIDIC WASH(4,1)\|ACTIVATED CARBON PURIFICATION(4,1)\|BACKWASH(4,1)\|BITUMINOUS COAL(4,1)\|CAPITAL INVESTMENT(4,1)\|COMPLETION(4,1)\|CRUSHING(4,1)\|DISPOSAL(4,1)\|EFFLUENT(4,1)\|ELEMENTAL PHOSPHORIC ACID(4,1)\|EXCESS SALT(4,1)\|EXPERIMENTATION(4,1)\|FOOD PRODUCTION(4,1)\|IMPURITE(4,1)\|INFLUX(4,1)\|LIGNITE(4,1)\|NEUTRALIZING(4,1)\|OCCASION(4,1)\|\|(US4299805)\|ACTIVATED CARBON(100,63)\|PHOSPHORIC ACID(100,43)\|BROWN PHOSPHORIC ACID(100,12)\|IMPURITY(100,6)\|CARBON REGENERATION(100,2)\|PRODUCING WET(100,1)\|BROWN PHOSPHORIC ACID FILTRATION(92,4)\|BROWN RESIDUE(68,2)\|ALKALI HYDROXIDE(66,5)\|RESIDUAL BROWN PHOSPHORIC ACID(59,2)\|RESIDUAL ALKALI HYDROXIDE(57,1)\|AQUEOUS SOLUTION(55,7)\|RESIDUAL ALKALI(54,3)\|AQUEOUS ALKALI HYDROXIDE(54,1)\|ALKANOL AMMONIA(53,2)\|BROWN PHOSPHORIC ACID PURIFICATION(51,1)\|CAUSTIC CYCLE(50,1)\|DECOLORIZATION(45,1)\|ALKYL AMMONIA(39,2)\|ALKALI CARBONATE(38,2)\|ALKALI HYDROXIDE AQUEOUS SOLUTION(38,1)\|MINERAL ACID DIGESTION(38,1)\|MINERAL ACID(37,10)\|ACID RESIDUE(34,1)\|PHOSPHORIC ACID PURIFICATION(31,1)\|AQUEOUS ALKALI(30,2)\|BASIC AQUEOUS SOLUTION(28,1)\|AMMONIUM HYDROXIDE(24,1)\|RECYCLING(24,1)\|BASE CYCLE(23,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(23,1)\|ACID SOLUTION SEQUENTIAL BATCH(22,1)\|PORE SIZE(17,2)\|AQUEOUS ACID SOLUTION(15,1)\|ROCK(14,2)\|WASHING WATER(14,2)\|ACIDIC SOLUTION(14,1)\|MINERAL ACID SOLUTION(11,1)\|RED FUMING NITRIC ACID(9,2)\|SODIUM HYDROXIDE(9,2)\|DIGESTION DEBACTEROL(9,1)\|GYPSUM GROSS PARTICLE(9,1)\|PHOSPHATIC FERTILIZER(9,1)\|PHOTOMETRY COLORIMETRY(9,1)\|LIQUID PHASE(8,1)\|LIQUID PHASE ACTIVATED CARBON(8,1)\|PULVERIZE ROCK(8,1)\|THRICE REPEATED DRAINING(8,1)\|BROWN TINGE(7,1)\|CONTAMINANT VARIED MIX(7,1)\|NEUTRALIZE CRUDE(7,1)\|ROCK IMPURITY(7,1)\|UNDUE DETRIMENT(7,1)\|WET(5,8)\|MARGINAL ARROW(5,1)\|PETROLEUM ACID SLUDGE(5,1)\|RAW BROWN(5,1)\|TRICKLE BED(5,1)\|VIRGIN CAPACITY(5,1)\|ACTIVATED CARBON BED(4,3)\|BROWN ACID(4,2)\|GRADE PHOSPHORIC ACID(4,2)\|GREEN PHOSPHORIC ACID(4,2)\|PATHWAY(4,2)\|REFILLING(4,2)\|BROWN PRODUCTION(4,1)\|CAUSTIC SOLUTION(4,1)\|COMPLEX SILICATE(4,1)\|ELECTROTHERMAL PHOSPHORIC ACID(4,1)\|FLUSHING(4,1)\|GRANULAR CARBON(4,1)\|PAST FOOD(4,1)\|RESIDUAL PHOSPHORIC ACID BULK(4,1)\|SEPERATION(4,1)\|ACTIVATED CARBON PURIFICATION(3,1)\|BACKWASH(3,1)\|BITUMINOUS COAL(3,1)\|CAPITAL INVESTMENT(3,1)\|COMPLETION(3,1)\|CRUSHING(3,1)\|DISPOSAL(3,1)\|EFFLUENT(3,1)\|ELEMENTAL PHOSPHORIC ACID(3,1)\|EXCESS SALT(3,1)\|EXPERIMENTATION(3,1)\|FOOD PRODUCTION(3,1)\|INFLUX(3,1)\|LIGNITE(3,1)\|NEUTRALIZING(3,1)\|\|(CA1124031)\|ACTIVATED CARBON(100,30)\|PHOSPHORIC ACID(100,14)\|BROWN PHOSPHORIC ACID(100,8)\|ACTIVATED CARBON REGENERATION(100,3)\|ALKALI PHOSPHATE 3(100,3)\|IMPURITY(100,2)\|PRODUCING PHOSPHORIC ACID(100,2)\|PRODUCING WET(100,1)\|BROWN PHOSPHORIC ACID FILTRATION(97,4)\|ALKALI HYDROXIDE(77,4)\|BROWN RESIDUE(71,2)\|ALKANOL AMMONIA(71,1)\|AQUEOUS SOLUTION(66,5)\|BROWN H3PO(65,1)\|RESIDUAL BROWN PHOSPHORIC ACID(62,2)\|RESIDUAL ALKALI HYDROXIDE(60,1)\|RESIDUAL ALKALI(57,3)\|AQUEOUS ALKALI HYDROXIDE(56,1)\|BROWN PHOSPHORIC ACID PURIFICATION(54,1)\|ALKYL AMMONIA(53,1)\|CAUSTIC CYCLE(53,1)\|CRUDE BASE(53,1)\|ALKALI CARBONATE(51,1)\|DECOLORIZATION(48,1)\|MINERAL ACID(44,7)\|AQUEOUS ALKALI(43,1)\|ALKALI HYDROXIDE AQUEOUS SOLUTION(40,1)\|MINERAL ACID DIGESTION(40,1)\|ACID RESIDUE(35,1)\|BASIC AQUEOUS SOLUTION(29,1)\|AMMONIUM HYDROXIDE(25,1)\|ALKALI METAL RAW(24,1)\|BASE CYCLE(24,1)\|RESIDUAL ALKALI HYDROXIDE SOLUTION(24,1)\|ACID SOLUTION SEQUENTIAL BATCH(23,1)\|DEBACTEROL(23,1)\|WASHING WATER(18,1)\|AQUEOUS ACID SOLUTION(16,1)\|	(EP0004807)\|1. A process for regenerating activated carbon employed for removal of contamination from brown phosphoric acid or aqueous solution of crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by passing aqueous solution comprising 1% to 50% by weight of a base through said activated charcoal and subsequent thereto passing a 0.5 to 2.0N aqueous solution of mineral acid other than brown phosphoric acid through said activated carbon.\|2. In the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1-10 hours; washing the activated carbon with water to remove residual base; contacting the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1-16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|3. A process according to claim 2 where the base is an alkali hydroxide.\|4. A process according to claim 3 where the mineral acid is sulfuric acid.\|5. A process according to claim 3 where the activated carbon is granular.\|6. A process according to claim 3 where the alkali hydroxide is sodium hydroxide.\|7. A process according to claim 3 where the activated carbon is steeped in at least two sequential batches of alkali hydroxide solution.\|8. A process according to claim 3 where the activated carbon is washed with water subsequent to the removal of the mineral acid.\|9. A process according to claim 3 where subsequent to removal of residual alkali hydroxide solution the brown phosphoric acid is filtered through said carbon until its capacity is exhausted, and the activated carbon is washed and treated with the alkali hydroxide.\|10. A regenerated activated carbon having a mesh between 10 and 20 U.S. Standard and an ash content of less than 1 % by weight prepared by the process of claim 1.	(EP0004807)\|Disclosure of the invention:\|[0001] This invention relates to an improved process for recycling and regenerating activated carbon employed in the purification of phosphoric acid produced by the wet-process.\|Background of the invention:\|[0002] In the past food and pharmaceutical grade phosphoric acid or alkali metal phosphates including, for example, trisodium phosphate, sodium tripolyphosphate, tetrasodium pyrophosphate and disodium phosphate were prepared by the thermal acid method described in Slack, Phosphoric Acid, V. 1, pp. 927-966, Marcel Dekker, Inc. (1968). The phosphoric acid and phosphates used in food, pharmaceuticals and in the processing of foods and pharmaceuticals must within stringent limits be substantially free from arsenic, fluorides, heavy metals and general contaminants referred to as insolubles.\|[0003] The thermal process for producing food and pharmaceutical grade phosphoric acid produces extremely pure phosphoric acid, but requires extensive capital investment for equipment, a large input of energy and pollution control equipment. Until recently, the inability to confidently remove contaminants made electrothermal phosphoric acid prepared from elemental phosphorous the predominant source of pure phosphoric acid.\|[0004] The so-called wet process employing phosphate rock and sulfuric acid is well known in the art and described in Waggamen Phosphoric Acid, Phosphates and Phosphatic Fertilizer, pp. 174-209, Hafner Publishing Co. (2nd Ed., 1969). The wet process is also broad enough to include acids other than sulfuric, including nitrice and hydrochloric acid. This is described in Slack, Phosphoric Acid, V. 1, Part 2, pp. 889-926, Marcel Dekker, Inc. (1968).\|[0005] U.S. Patent No. 1,533,031 and French Patent Nos. 1,290,655 and 1,264,118 disclose the regeneration of carbon by base washing followed by acid washing.\|[0006] Many processes were proposed to remove the contaminants found in wet process phosphoric acid and substantially all the successful processes employ activated carbon. For example, see US-A-3,993,733; US-A-3,872,215: US-A-3,993,736; US-A-3,122,415; and GB-A-1,442,919. Unfortunately, the phosphate rock impurities deactivate the porous activated carbon and because sufficient of these impurities are inorganic, thermal regeneration of the activated carbon is unsuitable because phosphate glasses fuse to the pores of the activated carbon. Since the use of activated carbon was the key to so many successful processes for upgrading wet process phosphoric acid, however, some means to increase the life of the too quickly exhausted activated carbon was necessary, since mere disposal after only limited use is clearly economically unsatisfactory. Attempts were made to backwash the activated carbon with poor results. Washing with caustic as in British Patent ,,1103,224 at first seemed a satisfactory solution, but the activated carbon never returns to more than 90% of the immediately previous cycles capacity, so after four regenerations the capacity is reduced to about 66% of the virgin activated carbon and after ten regeneration cycles with caustic alone, the carbon is substantially exhausted.\|[0007] Clearly, unless inordinate quantities of activated carbon are to be employed a more efficient regeneration means is required to not only save the capital cost and operating of renewing the activated carbon, but also the labor employed in replacement.\|[0008] The process of this invention returns the activated carbon to a condition equivalent to its virgin capacity, it achieves the results required to make wet process phosphoric acid the equivalent of thermal elemental phosphoric acid, since processes using activated carbon now become commercially feasible.\|Detailed description of the invention:\|[0009] The nature and content of the impurities that poison the activated charcoal and necessitate its regeneration are only partially understood. They mostly comprise gypsum that continues to precipitate from the brown phosphoric acid. earth waxes, and humic acids together with heavy metal salts, for example, arsenic, lead and the like as well as fluoride salts and complex silicates. Indeed, the exact nature of the contaminants is difficult to state with precision since the composition of the raw phosphate rock will differ with the run of the mine and even more widely from mine to mine. Also, the sulfur employed to produce the sulfuric acid will itself contain various impurities that carry over to poison, clog or otherwise exhaust the activated carbon. In addition, the wearing of the crushing surfaces of processing equipment employed to pulverize the rock can also introduce impurites that appear in the brown acid. Thus, it is all the more remarkable that the process of this invention is useful in regenerating activated carbon containing such a varied mix of contaminants.\|[0010] In the production of brown acid, phosphate containing rock usually predominantly calcium phosphate is pulverized and digested with mineral acid. The rock material is a mixture of overburden, and organic material running through the veins. Generally, in the digestion sulfuric acid is employed which produces large quantities of calcium sulfate. This slowly precipitates as gypsum. Other mineral acids are suitable and on some occasions employed in the production of phosphoric acid. These other mineral acids also produce contaminants and physical deposits similar to those found in the process when sulfuric acid is employed, except of course, gypsum is for the most part absent. Since the principles of the regeneration process of this invention are independent of the acid employed, the process will be exemplified by means of the sulfuric wet process.\|[0011] Referring to the flow chart, the raw brown acid that usually comes from the wet process digestion is about 28% to 34% by weight (expressed in P 205 content). The brown acid is usually put through a separation step to remove gross particles of gypsum and often a solids contact unit clarifyer to further remove residual solids. This intermediate processing can also be employed to neutralize the crude phosphoric acid to alkali metal phosphates.\|[0012] At this point, many producers employ one or more activated carbon purification steps. In the purification, the brown phosphoric acid is by gravity or by pressure filtered through a bed or column of activated carbon. The activated carbon employed can be derived from bituminous coal, lignite, peat, coconut shells, from wood sources or from petroleum acid sludge, or coke and need not have any particular pore size or mesh size. Generally, the so-called liquid phase activated carbons are preferred since their pore size distribution is sufficiently large to allow for easy access of liquids to the interior of the pores. The gas phase activated carbons are suitable but require a slightly longer residence time of the material to be purified. The more preferred activated carbons are granular and have a total surface area of 500-1200 m2/g. One such carbon is sold as SGL Granular Carbon.\|[0013] In most cases, a residence time of from 1/3-3 hours in the activated carbon is satisfactory, while 1 1/2 hours is most desirable. When the existing phosphoric acid is no longer green, but starts to take on a brown tinge or if such a lengthy residence time is required that production is hampered or color specifications are exceeded, it is time to regenerate the carbon.\|[0014] The present invention is also directed to the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1 to 10 hours; washing the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1 to 16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|[0015] In its broadest aspects, the invention entails intermittent washing of the activated carbon with aqueous base and aqueous mineral acid. This acid-base treatment can be sequential or the activated carbon can be employed to filter phosphoric acid between treatment with either acid or base.\|[0016] The regeneration of the activated carbon is, however, preferably performed in accordance with the steps 1-17 set forth in the table. In the preferred process, the column or bed of activated carbon is drained of its contents and refilled with whatever solution is dictated by the next step, and that solution allowed to steep in the column or bed of activated carbon for the specified time usually from 1-10 hours, before proceeding to the next step. If plant conditions dictate it is, however, suitable to practice continuous influx and outflow, during all steps, if this continuous flusing is practical rather than the "drain-fill steep" preferred embodiment the contact time of water, base and acid, should be adjusted accordingly so they are equivalent to the residence time set forth in the preferred embodiment.\|[0017] It should be noted that a number of steps in the preferred process can suitably be eliminated without undue detriment to the activated carbon. These eleminated steps are indicated by the marginal arrows for example from step 2b to step 9a. Otherwise, it is generally preferred to follow the steps in sequence.\|[0018] Proceeding from step 11, when the green acid produced starts to show more than the desired level of contamination, the activated carbon bed or column is removed from service drained and filled with water as in step 1 a. After a contact time of from 1/4 to about 4 hours, the column or bed is drained, step 1 b, preferably collecting the effluent which is enriched in phosphoric acid. This water washing sequence is repeated as in steps 2a through 3b. As already stated a continuous flow water wash is nearly as satisfactory. What is desired is that the bulk of residual phosphoric acid is flushed from the activated carbon so that neutralization producing excess salts that could deteriorate the activated carbon does not occur when the caustic solution is employed.\|[0019] Then in step 4a, the activated carbon bed or column is loaded with a 1% to 50% by weight aqueous solution of base. By the term "base" it is meant a substance that in aqueous solution induces a pH of 8 and preferably 10. Suitable bases include alkali hydroxides, alkali carbonates, ammonia, lower alkylamines and lower alkanol amines. The preferred base is sodium hydroxide. This solution is allowed to remain in the bed or column for from 1/4 to 10 hours. The base solution is then drained from the bed or column. This can be repeated one or more times, but is not absolutely required.\|[0020] Again, a continuous flow for 1/4 to 10 hours such as in a trickle bed is satisfactory, but the steeping is preferred. The caustic is then rinsed from the bed or column as in step 7a in the same manner as in steps 1-3. While, one water wash is sufficient, it is preferred at least three water washings be employed.\|[0021] At this point, the bed or column can be either returned to operation step 10 or treated with the acid as in step 12 and as set forth below in detail. If returned to operation, the cycle steps 1-11 are repeated from 1 to 8 additional times or until the specification for the phosphoric acid shows by photometry colorimetry or other analytical means that excessive impurities are present in the green phosphoric acid. At that point, the activated carbon bed or column is then treated with acid subsequent to the water rinse following the caustic steep. The column or bed is filled with from 0.5 to 2ZN . aqueous mineral acid such as sulfuric, hydrochloric, or nitric acid although sulfuric acid is preferred. This solution is allowed to steep in the carbon bed or column for from 1/2 to 16 hours. A single fill without draining and refilling is generally preferred but a twice or thrice repeated draining and refilling is suitable, but not found to be necessary in most cases. The acid steep as all other operations in steps 1-17 is preferably conducted at ambient temperature, but temperatures from 20°C. to 60°C. are suitable. When the temperature exceeds 25°C. the time to conduct the regeneration is shortened proportionately and from 1-4 hours is in most cases found sufficient.\|[0022] The exact time period, of course, must be determined by some experimentation because of the wide variation in the chemical composition of phosphate rock raw material. After completing steps 12b, 13b or 14b where the spent acid is conveniently channeled to the rock digestion process, the activated carbon is preferably water washed as in steps 1-3 or by continuous flow as previously described. The water wash can be eliminated but this is not at all recommended since the green phosphoric acid becomes contaminated with sulfuric acid. This may, however, be satisfactory when fertilizer grade phosphoric acid is contemplated.\|[0023] The activated carbon obtained from the process of this invention after the caustic-rinse acid-rinse cycle steps 1-17 is novel in that it comprises an activated carbon having a surprisingly low ash, generally less than 1% as indicated by ASTM D-2866-70. The novel activated carbon is also characterized in that the size range of the activated carbon particles is substantially uniform and is within a range of 10-20 mesh U.S. Standard. This carbon being so uniquely low in ash and of a substantially uniform size is particularly suitable for operations where such properties are desirable as in the filtration of pharmaceutical products or intermediates.\|[0024] In the attached flow sheet, the solid lines indicate the most usual pathway in the production of wet process phosphoric acid. The dashed lines indicate optional pathways which may be employed by various users of the wet process without departing from the spirit or scope of this invention.\|TABLE 1\|	(EP0004807)\|Disclosure of the invention:\|[0001] This invention relates to an improved process for recycling and regenerating activated carbon employed in the purification of phosphoric acid produced by the wet-process.\|Background of the invention:\|[0002] In the past food and pharmaceutical grade phosphoric acid or alkali metal phosphates including, for example, trisodium phosphate, sodium tripolyphosphate, tetrasodium pyrophosphate and disodium phosphate were prepared by the thermal acid method described in Slack, Phosphoric Acid, V. 1, pp. 927-966, Marcel Dekker, Inc. (1968). The phosphoric acid and phosphates used in food, pharmaceuticals and in the processing of foods and pharmaceuticals must within stringent limits be substantially free from arsenic, fluorides, heavy metals and general contaminants referred to as insolubles.\|[0003] The thermal process for producing food and pharmaceutical grade phosphoric acid produces extremely pure phosphoric acid, but requires extensive capital investment for equipment, a large input of energy and pollution control equipment. Until recently, the inability to confidently remove contaminants made electrothermal phosphoric acid prepared from elemental phosphorous the predominant source of pure phosphoric acid.\|[0004] The so-called wet process employing phosphate rock and sulfuric acid is well known in the art and described in Waggamen Phosphoric Acid, Phosphates and Phosphatic Fertilizer, pp. 174-209, Hafner Publishing Co. (2nd Ed., 1969). The wet process is also broad enough to include acids other than sulfuric, including nitrice and hydrochloric acid. This is described in Slack, Phosphoric Acid, V. 1, Part 2, pp. 889-926, Marcel Dekker, Inc. (1968).\|[0005] U.S. Patent No. 1,533,031 and French Patent Nos. 1,290,655 and 1,264,118 disclose the regeneration of carbon by base washing followed by acid washing.\|[0006] Many processes were proposed to remove the contaminants found in wet process phosphoric acid and substantially all the successful processes employ activated carbon. For example, see US-A-3,993,733; US-A-3,872,215: US-A-3,993,736; US-A-3,122,415; and GB-A-1,442,919. Unfortunately, the phosphate rock impurities deactivate the porous activated carbon and because sufficient of these impurities are inorganic, thermal regeneration of the activated carbon is unsuitable because phosphate glasses fuse to the pores of the activated carbon. Since the use of activated carbon was the key to so many successful processes for upgrading wet process phosphoric acid, however, some means to increase the life of the too quickly exhausted activated carbon was necessary, since mere disposal after only limited use is clearly economically unsatisfactory. Attempts were made to backwash the activated carbon with poor results. Washing with caustic as in British Patent ,,1103,224 at first seemed a satisfactory solution, but the activated carbon never returns to more than 90% of the immediately previous cycles capacity, so after four regenerations the capacity is reduced to about 66% of the virgin activated carbon and after ten regeneration cycles with caustic alone, the carbon is substantially exhausted.\|[0007] Clearly, unless inordinate quantities of activated carbon are to be employed a more efficient regeneration means is required to not only save the capital cost and operating of renewing the activated carbon, but also the labor employed in replacement.\|[0008] The process of this invention returns the activated carbon to a condition equivalent to its virgin capacity, it achieves the results required to make wet process phosphoric acid the equivalent of thermal elemental phosphoric acid, since processes using activated carbon now become commercially feasible.\|Detailed description of the invention:\|[0009] The nature and content of the impurities that poison the activated charcoal and necessitate its regeneration are only partially understood. They mostly comprise gypsum that continues to precipitate from the brown phosphoric acid. earth waxes, and humic acids together with heavy metal salts, for example, arsenic, lead and the like as well as fluoride salts and complex silicates. Indeed, the exact nature of the contaminants is difficult to state with precision since the composition of the raw phosphate rock will differ with the run of the mine and even more widely from mine to mine. Also, the sulfur employed to produce the sulfuric acid will itself contain various impurities that carry over to poison, clog or otherwise exhaust the activated carbon. In addition, the wearing of the crushing surfaces of processing equipment employed to pulverize the rock can also introduce impurites that appear in the brown acid. Thus, it is all the more remarkable that the process of this invention is useful in regenerating activated carbon containing such a varied mix of contaminants.\|[0010] In the production of brown acid, phosphate containing rock usually predominantly calcium phosphate is pulverized and digested with mineral acid. The rock material is a mixture of overburden, and organic material running through the veins. Generally, in the digestion sulfuric acid is employed which produces large quantities of calcium sulfate. This slowly precipitates as gypsum. Other mineral acids are suitable and on some occasions employed in the production of phosphoric acid. These other mineral acids also produce contaminants and physical deposits similar to those found in the process when sulfuric acid is employed, except of course, gypsum is for the most part absent. Since the principles of the regeneration process of this invention are independent of the acid employed, the process will be exemplified by means of the sulfuric wet process.\|[0011] Referring to the flow chart, the raw brown acid that usually comes from the wet process digestion is about 28% to 34% by weight (expressed in P 205 content). The brown acid is usually put through a separation step to remove gross particles of gypsum and often a solids contact unit clarifyer to further remove residual solids. This intermediate processing can also be employed to neutralize the crude phosphoric acid to alkali metal phosphates.\|[0012] At this point, many producers employ one or more activated carbon purification steps. In the purification, the brown phosphoric acid is by gravity or by pressure filtered through a bed or column of activated carbon. The activated carbon employed can be derived from bituminous coal, lignite, peat, coconut shells, from wood sources or from petroleum acid sludge, or coke and need not have any particular pore size or mesh size. Generally, the so-called liquid phase activated carbons are preferred since their pore size distribution is sufficiently large to allow for easy access of liquids to the interior of the pores. The gas phase activated carbons are suitable but require a slightly longer residence time of the material to be purified. The more preferred activated carbons are granular and have a total surface area of 500-1200 m2/g. One such carbon is sold as SGL Granular Carbon.\|[0013] In most cases, a residence time of from 1/3-3 hours in the activated carbon is satisfactory, while 1 1/2 hours is most desirable. When the existing phosphoric acid is no longer green, but starts to take on a brown tinge or if such a lengthy residence time is required that production is hampered or color specifications are exceeded, it is time to regenerate the carbon.\|[0014] The present invention is also directed to the process of producing phosphoric acid or alkali phosphates, a method for regenerating activated carbon employed in the filtration of brown phosphoric acid or the crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by the steps of water washing the activated carbon to remove residual brown phosphoric acid or phosphate; contacting the activated carbon with an aqueous solution of a base where the solution is from 1% to 50% by weight in said base at a temperature of from 20°C. to 60°C. for a period of from 1 to 10 hours; washing the activated carbon with an aqueous solution of 0.5 to 2N mineral acid other than brown phosphoric acid at a temperature of from 20°C. to 60°C. for a period of 1 to 16 hours; removing the mineral acid from the activated carbon and resuming filtration of brown phosphoric acid.\|[0015] In its broadest aspects, the invention entails intermittent washing of the activated carbon with aqueous base and aqueous mineral acid. This acid-base treatment can be sequential or the activated carbon can be employed to filter phosphoric acid between treatment with either acid or base.\|[0016] The regeneration of the activated carbon is, however, preferably performed in accordance with the steps 1-17 set forth in the table. In the preferred process, the column or bed of activated carbon is drained of its contents and refilled with whatever solution is dictated by the next step, and that solution allowed to steep in the column or bed of activated carbon for the specified time usually from 1-10 hours, before proceeding to the next step. If plant conditions dictate it is, however, suitable to practice continuous influx and outflow, during all steps, if this continuous flusing is practical rather than the "drain-fill steep" preferred embodiment the contact time of water, base and acid, should be adjusted accordingly so they are equivalent to the residence time set forth in the preferred embodiment.\|[0017] It should be noted that a number of steps in the preferred process can suitably be eliminated without undue detriment to the activated carbon. These eleminated steps are indicated by the marginal arrows for example from step 2b to step 9a. Otherwise, it is generally preferred to follow the steps in sequence.\|[0018] Proceeding from step 11, when the green acid produced starts to show more than the desired level of contamination, the activated carbon bed or column is removed from service drained and filled with water as in step 1 a. After a contact time of from 1/4 to about 4 hours, the column or bed is drained, step 1 b, preferably collecting the effluent which is enriched in phosphoric acid. This water washing sequence is repeated as in steps 2a through 3b. As already stated a continuous flow water wash is nearly as satisfactory. What is desired is that the bulk of residual phosphoric acid is flushed from the activated carbon so that neutralization producing excess salts that could deteriorate the activated carbon does not occur when the caustic solution is employed.\|[0019] Then in step 4a, the activated carbon bed or column is loaded with a 1% to 50% by weight aqueous solution of base. By the term "base" it is meant a substance that in aqueous solution induces a pH of 8 and preferably 10. Suitable bases include alkali hydroxides, alkali carbonates, ammonia, lower alkylamines and lower alkanol amines. The preferred base is sodium hydroxide. This solution is allowed to remain in the bed or column for from 1/4 to 10 hours. The base solution is then drained from the bed or column. This can be repeated one or more times, but is not absolutely required.\|[0020] Again, a continuous flow for 1/4 to 10 hours such as in a trickle bed is satisfactory, but the steeping is preferred. The caustic is then rinsed from the bed or column as in step 7a in the same manner as in steps 1-3. While, one water wash is sufficient, it is preferred at least three water washings be employed.\|[0021] At this point, the bed or column can be either returned to operation step 10 or treated with the acid as in step 12 and as set forth below in detail. If returned to operation, the cycle steps 1-11 are repeated from 1 to 8 additional times or until the specification for the phosphoric acid shows by photometry colorimetry or other analytical means that excessive impurities are present in the green phosphoric acid. At that point, the activated carbon bed or column is then treated with acid subsequent to the water rinse following the caustic steep. The column or bed is filled with from 0.5 to 2ZN . aqueous mineral acid such as sulfuric, hydrochloric, or nitric acid although sulfuric acid is preferred. This solution is allowed to steep in the carbon bed or column for from 1/2 to 16 hours. A single fill without draining and refilling is generally preferred but a twice or thrice repeated draining and refilling is suitable, but not found to be necessary in most cases. The acid steep as all other operations in steps 1-17 is preferably conducted at ambient temperature, but temperatures from 20°C. to 60°C. are suitable. When the temperature exceeds 25°C. the time to conduct the regeneration is shortened proportionately and from 1-4 hours is in most cases found sufficient.\|[0022] The exact time period, of course, must be determined by some experimentation because of the wide variation in the chemical composition of phosphate rock raw material. After completing steps 12b, 13b or 14b where the spent acid is conveniently channeled to the rock digestion process, the activated carbon is preferably water washed as in steps 1-3 or by continuous flow as previously described. The water wash can be eliminated but this is not at all recommended since the green phosphoric acid becomes contaminated with sulfuric acid. This may, however, be satisfactory when fertilizer grade phosphoric acid is contemplated.\|[0023] The activated carbon obtained from the process of this invention after the caustic-rinse acid-rinse cycle steps 1-17 is novel in that it comprises an activated carbon having a surprisingly low ash, generally less than 1% as indicated by ASTM D-2866-70. The novel activated carbon is also characterized in that the size range of the activated carbon particles is substantially uniform and is within a range of 10-20 mesh U.S. Standard. This carbon being so uniquely low in ash and of a substantially uniform size is particularly suitable for operations where such properties are desirable as in the filtration of pharmaceutical products or intermediates.\|[0024] In the attached flow sheet, the solid lines indicate the most usual pathway in the production of wet process phosphoric acid. The dashed lines indicate optional pathways which may be employed by various users of the wet process without departing from the spirit or scope of this invention.\|TABLE 1\|	Family Number\|(1081365)\|1081365\|Object of Invention\|(CA1124031 A)\|Abstract of the Disclosure In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali (...) \|(EP---4807 A3)\|In a process tor regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali (...) \|(EP---4807 A2)\|In a process tor regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali (...) \|(US4299805 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3 PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali (...) \|Abstract\|(AU-520262 B2)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(CA1124031 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrocloric, or nitric acid, again washed with water to remove residual acid and returned to service. Usually, the acid steep need not be employed with every base cycle to maintain good decolorization, although if desired the acid steep can be used with each caustic cycle.\|(DE2962375 D1)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(DK7901284 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(EP---4807 B1)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.\|(IT7948527 A0)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(JP54133498 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|(US4299805 A)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitric acid, again washed with water to remove residual acid and returned to service. Usually, the acid steep need not be employed with every base cycle to maintain good decolorization, although if desired the acid steep can be used with each caustic cycle.\|(ZA7901501 B)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.(From EP0004807 A2)\|Independent Claims\|(EP---4807 B1)\|1. A process for regenerating activated carbon employed for removal of contamination from brown phosphoric acid or aqueous solution of crude alkali metal phosphates derived therefrom comprising regenerating said activated carbon by alkali treatment, characterized by passing aqueous solution comprising 1% to (...) \|(EP---4807 A2)\|1. A process for regenerating activated carbon employed for removal of contamination from brown phosphoric acid or aqueous solution of crude alkali metal phosphates derived therefrom comprising passing aqueous solution comprising 1% to 50% by weight of a base through said activated charcoal and subsequent thereto (...) \|	Chemical engineering\|Materials, metallurgy	C01B-025/235\|C01B-025/30/8\|C01B-032/36		C01B-025/235\|C01B-025/30/8\|C01B-032/36	B01J-020/34\|C01B-025/234\|C01B-025/235\|C01B-025/30\|C01B-031/08	B01J-020/34\|C01B-025/16\|C01B-025/22\|C01B-025/234\|C01B-025/235\|C01B-025/30\|C01B-031/08\|C01B-031/12	PCLO=423321100	PCLO=423321000R PCLX=252412000	WO200579977\|CN102417178\|WO200066490\|CN117160184\|CN116395689\|CN113713762\|CN113247895\|CN113247895\|CN103896267\|US20100111811\|US20060223701\|CN116585848B\|US20070060476\|US7569514\|US7119047\|DE4222524\|US4822765\|US4761284\|US4558022\|US4495165\|US4503022\|US4407725\|US4407725	WO200579977 44555513 WHO=Examiner SELF=N CAT=Y\|CN102417178 7612130 WHO=Examiner SELF=N CAT=X\|WO200066490 1420164 WHO=Examiner SELF=N CAT=X\|CN117160184 107597685 WHO=Examiner SELF=N CAT=A\|CN116395689 105666606 WHO=Examiner SELF=N CAT=A\|CN113713762 97352655 WHO=Examiner SELF=N CAT=A\|CN113247895 95650355 WHO=Examiner SELF=N CAT=A\|CN113247895 95650355 WHO=Examiner SELF=N CAT=A\|CN103896267 66514074 WHO=Examiner SELF=N CAT=A\|US20100111811 15025702 WHO=Examiner SELF=N CAT=103\|US20060223701 43493001 WHO=Examiner SELF=N CAT=103\|CN116585848B 106130958 WHO=Examiner SELF=N\|US20070060476 43493001 WHO=Examiner SELF=N\|US7569514 43493001 WHO=Applicant SELF=N\|US7119047 43493001 WHO=Examiner SELF=N\|DE4222524 13017496 WHO=Examiner SELF=N\|US4822765 42614360 WHO=Examiner SELF=N\|US4761284 42614360 WHO=Examiner SELF=N\|US4558022 198388 WHO=Examiner SELF=Y\|US4495165 14627359 WHO=Examiner SELF=N\|US4503022 42527050 WHO=Examiner SELF=N\|US4407725 42501230 WHO=Examiner SELF=N\|US4407725 42501230 WHO=Examiner SELF=N	GB1103224\|FR2234228\|US3186793\|US3944513\|DE2206706\|US3720626\|GB1103224\|FR1290665\|GB-934695\|US1533031\|FR-481511	GB1103224 2259233 WHO=Examiner SELF=N CAT=A CAT=D\|FR2234228 12450784 WHO=Examiner SELF=N CAT=A\|US3186793 41868616 WHO=Examiner SELF=N CAT=A\|US3944513 42279640 WHO=Examiner SELF=N\|DE2206706 12367549 WHO=Examiner SELF=N\|US3720626 2339106 WHO=Examiner SELF=N\|GB1103224 2259233 WHO=Examiner SELF=N\|FR1290665 16545164 WHO=Examiner SELF=N\|GB-934695 17766161 WHO=Examiner SELF=N\|US1533031 40387123 WHO=Examiner SELF=N\|FR-481511 15856956 WHO=Examiner SELF=N		FR1290665; GB1103224; US3720626; US3944513\|\|\|\|\|DE2206706; US1533031; FR-481511; GB-934695; GB1103224; US3186793; FR2234228\|\|\|	(EP0004807)\|Search Report references [Examiner]\|-CHEMICAL ABSTRACTS, Vol. 87, no. 24, 12 December 1977 Abstract no. 188820r, page 267, column 1 Columbus, (Ohio), USA, M. BECCARI et al.: "Chemical regeneration of granular activated carbon" & EFFLUENT WATER TREATMENT JOURNAL 17 (6) 1977, pages 287, 290-295.\|-JOURNAL OF APPLIED CHEMISTRY OF THE USSR, Vol. 51, no. 8, part 1, August 1978, New York, USA, N.A. YAKUBENYA et al.: "Regeneration of active carbon used for purification of waste gases during production of synthetic fibers", pages 1683-1685.\|\|\|\|\|\|\|\|\|	EXPIRED	(EP0004807)\|EXPIRED\|(US4299805)\|EXPIRED\|(DE2962375)\|LAPSED\|(JPS54-133498)\|LAPSED\|(CA1124031)\|EXPIRED\|(AU520262)\|EXPIRED\|(ZA791501)\|EXPIRED\|(DK128479)\|LAPSED\|(IT7948527)\|LAPSED	DEAD	(EP0004807)\|DEAD\|(US4299805)\|DEAD\|(DE2962375)\|DEAD\|(JPS54-133498)\|DEAD\|(CA1124031)\|DEAD\|(AU520262)\|DEAD\|(ZA791501)\|DEAD\|(DK128479)\|DEAD\|(IT7948527)\|DEAD	(EP0004807)\|LEGAL DETAILS FOR EP0004807\|Actual or expected expiration date=1999-03-26\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-03-26\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP79400191\|Application date=1979-03-26\|Standardized application number=1979EP-0400191\|Event publication date=1979-08-21\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=1979-09-03\|Event code=EP/PUAL\|Event group=Examination events\|SEARCH REPORT DESPATCHED\|Publication of search report\|Original code: 0009013\|Event publication date=1979-10-17\|Event code=EP/A2\|Event group=Examination events\|Application published without search report\|Publication country=EP\|Publication number=EP0004807\|Publication stage code=A2\|Publication date=1979-10-17\|Standardized publication number=EP---4807\|Event publication date=1979-10-17\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=BE CH DE FR GB LU NL SE\|Event publication date=1979-10-31\|Event code=EP/A3\|Event indicator=Pos\|Event group=Examination events\|Published search report\|Publication country=EP\|Publication number=EP0004807\|Publication stage code=A3\|Publication date=1979-10-31\|Standardized publication number=EP---4807\|Event publication date=1979-10-31\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=BE CH DE FR GB LU NL SE\|Event publication date=1980-03-05\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Event publication date=1982-01-30\|Event code=EP/GRAA\|Event indicator=Pos\|Event group=Examination events\|(EXPECTED) GRANT\|Original code: 0009210\|Event publication date=1982-03-31\|Event code=EP/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent specification\|Publication country=EP\|Publication number=EP0004807\|Publication stage code=B1\|Publication date=1982-03-31\|Standardized publication number=EP---4807\|Event publication date=1982-03-31\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=BE CH DE FR GB LU NL SE\|Event publication date=1982-07-12\|Event code=EP/KL\|Event group=Corrections\|Correction list\|82/04\|Event publication date=1999-03-26\|Event code=EP/EEDX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent has expired\|Event publication date=2016-09-14\|Event code=EP/PLBE\|Event indicator=Pos\|Event group=No opposition filed\|NO OPPOSITION FILED WITHIN TIME LIMIT\|Original code: 0009261\|Event publication date=2016-09-14\|Event code=EP/STAANOPP\|Event indicator=Pos\|Event group=No opposition filed Event indicating In Force\|No opposition filed within time limit\|Original code: STAA\|MEMBER STATE LEGAL DETAILS FOR BE\|Actual or expected expiration date=1986-03-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BE\|Event publication date=1984-12-31\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1984-12-31\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=BE\|Event publication date=1986-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=BE\|Event publication date=1986-09-30\|Event code=EP/BERE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|BE: Lapsed\|BE: Dechu\|OWNER:CALGON CARBON CORP.\|Effective date of the event=1986-03-31\|Corresponding cc:\|Designated or member state=BE\|MEMBER STATE LEGAL DETAILS FOR CH\|Actual or expected expiration date=1984-03-31\|Legal state=DEAD\|Status=EXPIRED\|Corresponding cc:\|Designated or member state=CH\|Event publication date=1983-01-31\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1983-01-31\|Year of payment of annual fees=5\|Corresponding cc:\|Designated or member state=CH\|Event publication date=1984-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=CH\|Event publication date=1984-11-30\|Event code=EP/REG\|Event code=CH/PL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent ceased\|Loeschung/radiation/radiazion\|Corresponding cc:\|Designated or member state=CH\|MEMBER STATE LEGAL DETAILS FOR DE2962375\|Actual or expected expiration date=1986-12-02\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE Corresponding appl: DE2962375\|Application date in the designated or member state=1979-03-26\|Application number in the designated or member state=1979DE-2962375\|Corresponding cc:\|Designated or member state=DE Corresponding pat: DE2962375\|Publication stage code in the designated or member state=D1\|Publication date in the designated or member state=1982-05-06\|Publication number in the designated or member state=DE2962375\|Event publication date=1982-05-06\|Event code=EP/REF\|Event group=Entry into national phase\|Corresponds to:\|Corresponding cc:\|Designated or member state=DE\|Event publication date=1984-01-31\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1984-01-31\|Year of payment of annual fees=6\|Corresponding cc:\|Designated or member state=DE\|Event publication date=1986-12-02\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR FR\|Actual or expected expiration date=1986-11-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=FR\|Event publication date=1984-11-29\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1984-11-29\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=FR\|Event publication date=1985-12-27\|Event code=EP/REG\|Event code=FR/CD\|Event group=Change of name or address Reassignment\|Reference to a national code\|Change of name or company name\|Changement de nom de denomination\|Corresponding cc:\|Designated or member state=FR\|Event publication date=1986-11-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=FR\|Event publication date=1987-01-23\|Event code=EP/REG\|Event code=FR/ST\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Notification of lapse\|Constatation de decheances\|Corresponding cc:\|Designated or member state=FR\|MEMBER STATE LEGAL DETAILS FOR GB\|Actual or expected expiration date=1986-11-12\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GB\|Event publication date=1986-11-12\|Event code=EP/GBPC\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|GB: European patent ceased through non-payment of renewal fee\|Corresponding cc:\|Designated or member state=GB\|Event publication date=1988-11-17\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=GB\|MEMBER STATE LEGAL DETAILS FOR LU\|Actual or expected expiration date=1983-03-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LU\|Event publication date=1982-12-22\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1982-12-22\|Year of payment of annual fees=5\|Corresponding cc:\|Designated or member state=LU\|Event publication date=1983-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LU\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=1983-10-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NL\|Event publication date=1983-10-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=NL\|Event publication date=1983-11-16\|Event code=EP/NLV4\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|NL: Lapsed or anulled due to non-payment of the annual fee\|NL: Vervallen wegens niet betalen van een jaarcijns\|Corresponding cc:\|Designated or member state=NL\|MEMBER STATE LEGAL DETAILS FOR SE\|Actual or expected expiration date=1987-02-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SE Corresponding appl: SE79400191.7\|Event publication date=1984-03-31\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=1984-03-31\|Year of payment of annual fees=6\|Corresponding cc:\|Designated or member state=SE\|Event publication date=1986-03-27\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Corresponding cc:\|Designated or member state=SE\|Event publication date=1995-01-31\|Event code=EP/EUG\|Event indicator=Neg\|Event group=Event indicating Not In Force\|SE: European patent has lapsed\|SE: Europeiskt patent har upphoert att gaella\|Effective date of the event=1987-02-23\|Corresponding cc:\|Designated or member state=SE\|(US4299805)\|LEGAL DETAILS FOR US4299805\|Actual or expected expiration date=1998-11-10\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-08-21\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US06068316\|Application date=1979-08-21\|Standardized application number=1979US-06068316\|Event publication date=1979-08-21\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:HELLER, GREGORY\|Event publication date=1979-08-21\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1103\|Event publication date=1979-08-21\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: C1193CA\|Event publication date=1979-08-21\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: UNDISCOUNTED\|Event publication date=1979-08-21\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=1980-02-06\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=1980-02-06\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=1981-05-08\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=1981-05-08\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=1981-07-21\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=1981-07-21\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST.\|Assignors:TIGGELBECK DONALD D;WELLS BRUCE D.\|Reel/frame:003884/0398\|OWNER:CALGON CORPORATION ROUTE 60 & CAMPBELLS RUN RD. RO\|Effective date of the event=1978-03-28\|Event publication date=1981-07-21\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:TIGGELBECK DONALD D;WELLS BRUCE D.\|Reel/frame:003884/0398\|OWNER:CALGON CORPORATION ROUTE 60 & CAMPBELLS RUN RD. RO\|Effective date of the event=1978-03-28\|Event publication date=1981-11-06\|Event code=US/N066\|Event group=Payment or non-payment notifications\|Notice of balance of issue fee due (pto-1031) - charged to deposit account\|Event publication date=1981-11-10\|Event code=US/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Patents Granted before 2001-04-15\|Publication country=US\|Publication number=US04299805\|Publication stage code=A\|Publication date=1981-11-10\|Standardized publication number=US4299805\|Event publication date=1981-11-10\|Event code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=1984-12-21\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|CHANGE OF NAME\|Assignor:CALGON CORPORATION\|Reel/frame:004345/0918\|OWNER:CALGON CARBON CORPORATION\|Effective date of the event=1982-06-24\|Event publication date=1985-05-01\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|SECURITY INTEREST\|Assignor:CALGON CARBON CORPORATION\|Reel/frame:004398/0398\|OWNER:BANKERS TRUST COMPANY\|Effective date of the event=1985-04-19\|Event publication date=1989-01-09\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|RELEASED BY SECURED PARTY\|Assignor:BANKERS TRUST COMPANY\|Reel/frame:005017/0627\|OWNER:CALGON CARBON CORPORATION\|Effective date of the event=1988-09-01\|Event publication date=1998-11-10\|Event code=US/EEDX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent has expired\|(DE2962375)\|LEGAL DETAILS FOR DE2962375\|Actual or expected expiration date=1986-12-02\|Legal state=DEAD\|Status=LAPSED\|Event publication date=1979-03-26\|Event code=DE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=DE DE2962375\|Application date=1979-03-26\|Standardized application number=1979DE-2962375\|Event publication date=1982-05-06\|Event code=DE/D1\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant (no unexamined application published) patent law 81\|Patenterteilung (keine 0s) patg. 81\|Publication country=DE\|Publication number=DE2962375\|Publication stage code=D1\|Publication date=1982-05-06\|Standardized publication number=DE2962375\|Event publication date=1986-12-02\|Event code=DE/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|Event publication date=1987-03-19\|Event code=DE/8339\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Ceased/non-payment of the annual fee\|Wegen nichtz. d. jahresgeb. erloschen\|(JPS54-133498)\|LEGAL DETAILS FOR JPS54-133498\|Actual or expected expiration date=1988-10-17\|Legal state=DEAD\|Status=LAPSED\|Event publication date=1979-03-27\|Event code=JP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=JP JP3515679\|Application date=1979-03-27\|Standardized application number=1979JP-0035156\|Event publication date=1979-10-17\|Event code=JP/A\|Event group=Examination events\|Published application\|Publication country=JP\|Publication number=JPS54133498\|Publication stage code=A\|Publication date=1979-10-17\|Standardized publication number=JP54133498\|Event publication date=1988-10-17\|Event code=JP/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(CA1124031)\|LEGAL DETAILS FOR CA1124031\|Actual or expected expiration date=1999-05-25\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-02-23\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA322199\|Application date=1979-02-23\|Standardized application number=1979CA-0322199\|Event publication date=1982-05-25\|Event code=CA/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent granted\|Publication country=CA\|Publication number=CA1124031\|Publication stage code=A\|Publication date=1982-05-25\|Standardized publication number=CA1124031\|Event publication date=1999-05-25\|Event code=CA/MKEX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Expiry\|(AU520262)\|LEGAL DETAILS FOR AU520262\|Actual or expected expiration date=1998-01-21\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-03-22\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU4533979\|Application date=1979-03-22\|Standardized application number=1979AU-0045339\|Event publication date=1979-10-04\|Event code=AU/A\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU4533979\|Publication stage code=A\|Publication date=1979-10-04\|Standardized publication number=AU7945339\|Event publication date=1982-01-21\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent preceeded by A1\|Publication country=AU\|Publication number=AU520262\|Publication stage code=B2\|Publication date=1982-01-21\|Standardized publication number=AU-520262\|Event publication date=1999-03-22\|Event code=AU/EEDX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent has expired\|(ZA791501)\|LEGAL DETAILS FOR ZA791501\|Actual or expected expiration date=1999-03-29\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=1979-03-29\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA791501\|Application date=1979-03-29\|Standardized application number=1979ZA-0001501\|Event publication date=1980-11-26\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA791501\|Publication stage code=B\|Publication date=1980-11-26\|Standardized publication number=ZA7901501\|Event publication date=1999-03-29\|Event code=ZA/EEDX\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent has expired\|(DK128479)\|LEGAL DETAILS FOR DK128479\|Actual or expected expiration date=1984-10-01\|Legal state=DEAD\|Status=LAPSED\|Event publication date=1979-03-29\|Event code=DK/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=DK DK128479\|Application date=1979-03-29\|Standardized application number=1979DK-0001284\|Event publication date=1979-10-01\|Event code=DK/A\|Event group=Examination events\|Published application\|Publication country=DK\|Publication number=DK128479\|Publication stage code=A\|Publication date=1979-10-01\|Standardized publication number=DK7901284\|Event publication date=1984-10-01\|Event code=DK/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IT7948527)\|LEGAL DETAILS FOR IT7948527\|Actual or expected expiration date=1999-03-29\|Legal state=DEAD\|Status=LAPSED\|Event publication date=1979-03-29\|Event code=IT/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IT IT4852779\|Application date=1979-03-29\|Standardized application number=1979IT-0048527\|Event publication date=1979-03-29\|Event code=IT/A0\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=IT\|Publication number=IT7948527\|Publication stage code=A0\|Publication date=1979-03-29\|Standardized publication number=IT7948527\|Event publication date=1999-03-29\|Event code=IT/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned	(EP0004807)\|Contracting States: DE, SE, BE, CH, LU, GB, FR, NL		https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=Ha67aj7xeb/nOPB6GlyZ+WkyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP0000000000059790&ekey=2273&xpn=EP---4807&kind=B1	https://register.epo.org/application?number=EP79400191	https://permalink.orbit.com/RenderStaticFirstPage?XPN=NVVyZEDoMGrdGqGyRhNS9XfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(US4299805)\|US\|\|(EP0004807)\|US\|(EP0004807)\|US\|(CA1124031)\|US	(US4299805)\|NAME=Calgon Corporation , CITY=Pittsburgh , STATE=PA , COUNTRY=US , ATYP=US Company\|(IT7948527)\|NAME=CALGON CORPORATION A ROBINSON TOWNSHIP PENNSYLVANIA\|(EP0004807)\|NAME=CALGON CORPORATION Route 60-Campbell's Run Road , CITY=Robinson TownshipPennsylvania 15205 , COUNTRY=US , REG=00212230\|(EP0004807)\|NAME=CALGON CORPORATION Route 60-Campbell's Run Road , CITY=Robinson TownshipPennsylvania 15205 , COUNTRY=US , REG=00212230\|(CA1124031)\|NAME=CALGON CORPORATION 5400 Campbells Run Road , CITY=PITTSBURGH , STATE=PA , POSTCODE=15205 , COUNTRY=US	(EP0004807)\|FR\|(EP0004807)\|FR\|(EP0004807)\|FR\|\|(CA1124031)\|CA	(EP0004807)\|NAME=Corre, Jacques Denis Paul;Cabinet Regimbeau 26, Avenue Kléber , CITY=75116 Paris , COUNTRY=FR , REG=00014911\|(EP0004807)\|NAME=Corre, Jacques Denis Paul, et al Cabinet Regimbeau 26, Avenue Kléber F-75116 Paris , COUNTRY=FR\|(EP0004807)\|NAME=Corre, Jacques Denis Paul;Cabinet Regimbeau 26, Avenue Kléber , CITY=75116 Paris , COUNTRY=FR , REG=00014911\|(US4299805)\|NAME=Katz Martin L. NAME=Riedl Edmunde D. NAME=Olson R. Brent\|(CA1124031)\|NAME=GOUDREAU, GAGE & ASSOCIATES , COUNTRY=CA	(EP0004807)\|US; US\|\|(EP0004807)\|US; US\|(US4299805)\|US\|\|\|(CA1124031)\|US; US\|\|\|\|	(EP0004807)\|NAME=Wells, Bruce Douglas 74 Mayfair Drive, CITY=PittsburghPennsylvania 15228, COUNTRY=US \|NAME=Tiggelbeck, Donald David 204 Seneca Drive, CITY=PittsburghPennsylvania 15228, COUNTRY=US\|(EP0004807)\|NAME=Wells, Bruce Douglas\|NAME=Tiggelbeck, Donald David\|(EP0004807)\|NAME=Wells, Bruce Douglas 74 Mayfair Drive, CITY=PittsburghPennsylvania 15228, COUNTRY=US \|NAME=Tiggelbeck, Donald David 204 Seneca Drive, CITY=PittsburghPennsylvania 15228, COUNTRY=US\|(US4299805)\|NAME=Wells Bruce D., CITY=Pittsburgh, STATE=PA , COUNTRY=US\|(DE2962375)\|NAME=WELLS, BRUCE DOUGLAS\|NAME=TIGGELBECK, DONALD DAVID\|(JPS54-133498)\|NAME=BURUUSU DAGURASU UERUSU\|NAME=DONARUDO DEIBUITSUDO TEIGERUBE\|(CA1124031)\|NAME=WELLS, BRUCE D., COUNTRY=US \|NAME=TIGGELBECK, DONALD D., COUNTRY=US\|(AU520262)\|NAME=B.D. WELLS\|NAME=D.D. TIGGELBECK\|(AU4533979)\|NAME=BRUCE DOUGLAS WELLS\|NAME=DONALD DAVID TIGGELBECK\|(ZA791501)\|NAME=TIGGELBECK D\|NAME=WELLS B\|(DK128479)\|NAME=WELLS B D\|NAME=TIGGELBECK D D	(US4299805)\|2\|\|	2	9		BANKERS TRUST; FROM 1985-04-19; TO 1988-09-01		(DE2962375)\|EP79400191	(EP0004807)\|Number of Claims: NCL=10\|\|(EP0004807)\|Number of Claims: NCL=10\|\|(US4299805)\|Number of Claims: NCL=14\|Number of Drawings: NDR=2\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1,2\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: Vertiz O. R.\|Art Unit.: ART =113\|\|(CA1124031)\|Number of Claims: NCL=14\|\|(ZA791501)\|Number of Claims: NCL=1\|		(EP0004807)\|ENGLISH (ENG)	(CA1124031)\|Patent\|(DE2962375)\|Patent\|(EP---4807)\|Patent\|(AU-520262)\|Patent\|(US4299805)\|Patent\|(ZA7901501)\|Patent\|(EP---4807)\|Patent\|(EP---4807)\|Patent\|(JP54133498)\|Patent\|(AU7945339)\|Patent\|(DK7901284)\|Patent\|(IT7948527)\|Patent	Titre: (EP0004807)\|Regeneration of carbon employed in the wet process production of phosphoric acid Résumé: (EP0004807)\|In a process for regenerating the activated carbon and in the purification of brown phosphoric acid or alkali phosphates obtained via the so-called wet process employing mineral acid digestion of crushed phosphate rock, the activated carbon used to filter brown H3PO4 is removed from service, washed with water, the initial washings being recovered to reclaim phosphoric acid, and then steeped in a basic aqueous solution, e.g., aqueous alkali hydroxide, alkali carbonate, ammonium hydroxide, loweralkyl amines or loweralkanol amines. After again water washing the activated carbon, to remove residual base, the activated carbon is either returned to service or steeped in an aqueous solution of mineral acid, e.g., sulfuric, hydrochloric, or nitrid acid, again washed with water to remove residual acid and returned to service.	22	Abstract	gpt-4o-mini	no	The article focuses on the regeneration of activated carbon in the production of phosphoric acid, which does not relate to accelerated weathering or CO₂ capture.
25	CN202110935649	CN202110935649	CN113683197	97182255	CN113683197 A 2021-11-23 [CN113683197]	2021-08-16	2021-08-16	2021-11-23		(CN113683197)\|2023-06-23	(CN113683197)\|Efficient nitrogen and phosphorus removal anti-blocking constructed wetland system	(CN113683197)\|The invention discloses an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system, and relates to the technical field of constructed wetland construction. The system comprises an aeration reoxygenation chamber, an enhanced carbon removal chamber, an enhanced nitrogen removal chamber, an enhanced phosphorus removal chamber, a sludge sedimentation tank and the like. A water inlet channel is mainly used for uniformly distributing water and collecting purified water. The aeration reoxygenation chamber is a main body unit for water quality purification and mainly comprises an aeration device, composite filler and plants, and when a polluted water body flows through the unit module, the water quality can be purified by virtue of the composite filler, soil filtration, and activities of aquatic plants, high-efficiency microorganisms and the like. According to the water quality of inlet water and the water quality target needing to be achieved, different concentrated and matched fillers can be selected, so that the enhanced carbon removal chamber, the enhanced nitrogen removal chamber, the enhanced phosphorus removal chamber and the sludge sedimentation tank which are designed and obtained can effectively remove nitrogen, phosphorus, heavy metal, impurity sludge and the like in the water body.	ANHUI XINYU ECOLOGICAL INDUSTRY	(CN113683197)\|ANHUI XINYU ECOLOGICAL IND CO LTD ([CN])	ZHANG YOUDE\|HE JIANJUN\|DAI CAOPEI\|ZHANG TIANTIAN	(CN113683197)\|ZHANG YOUDE\|HE JIANJUN\|DAI CAOPEI\|ZHANG TIANTIAN	(CN113683197)\|WANG XIAOJUN;Hefei Daozhi Intellectual Property Agency Co., Ltd.\|Reg. Nb: 34130	(CN113683197)\|However, the conventional subsurface flow constructed wetland has insufficient dissolved oxygen and the denitrification effect is difficult to meet the strict emission standard, so the current challenges are to effectively balance the oxygen demand and input in the artificial system under the condition of reducing the cost and how to design a system which can ensure the treatment efficiency and keep the system simple and economic in the aspects of layout, construction and maintenance.\|	(CN113683197)\|1. An efficient nitrogen and phosphorus removal anti-blocking constructed wetland system is characterized by comprising an aeration reoxygenation chamber (1), an enhanced decarbonization chamber (2), an enhanced denitrification chamber (3) and an enhanced phosphorus removal chamber (4), wherein a water inlet channel (5) is arranged on the front side of the aeration reoxygenation chamber (1), an observation chamber (6) is arranged between the enhanced decarbonization chamber (2) and the enhanced denitrification chamber (3), and a water drainage channel (7) is arranged on the rear side of the enhanced phosphorus removal chamber (4);the water inlet channel (5) is communicated with the aeration reoxygenation chamber (1) through a first overflow pipe (9), a main pipe (10) and branch pipes are arranged below the aeration reoxygenation chamber (1), and the outer end of the main pipe (10) is connected with an aeration device;a first composite filler (12) is filled in the aeration reoxygenation chamber (1), the first composite filler (12) comprises at least two of large-particle-size crushed stone, gravel, volcanic rock and suspended ceramsite, and the suspended ceramsite contains immobilized microorganisms;the enhanced decarbonization chamber (2) is positioned at the rear side of the aeration reoxygenation chamber (1) and is communicated with the aeration reoxygenation chamber through a second overflow pipe (13), a second composite filler (14) is filled in the enhanced decarbonization chamber (2), and the second composite filler (14) comprises gravel, broken stone and limestone;the enhanced denitrification chamber (3) is positioned at the rear side of the observation chamber (6), a third overflow pipe (15) and a first reserved water pipe (16) are respectively arranged at two sides of the observation chamber (6), the third overflow pipe (15) is communicated with the enhanced decarbonization chamber (2) and the observation chamber (6), the first reserved water pipe (16) is arranged at the bottom and is communicated with the observation chamber (6) and the enhanced denitrification chamber (3); a third composite filler (17) is filled in the enhanced denitrification chamber (3), and the third composite filler (17) comprises gravel, biochar and broken stone;the enhanced phosphorus removal chamber (4) is positioned at the rear side of the enhanced nitrogen removal chamber (3), the enhanced phosphorus removal chamber (4) is communicated with the enhanced nitrogen removal chamber (3) through a fourth overflow pipe (18), a fourth composite filler (19) is filled in the enhanced phosphorus removal chamber, the fourth composite filler (19) comprises gravel, zeolite, coal ash and crushed stone, and the enhanced phosphorus removal chamber (4) is communicated with the drainage channel (7) through a second reserved water pipe (20) arranged at the bottom;the bottom of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced dephosphorization chamber (4) is of a slope structure, a plurality of sludge discharge pipes (26) are pre-buried at the bottoms of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced dephosphorization chamber (4), the sludge discharge pipes (26) are laid on the slope, a plurality of holes are formed in the sludge discharge pipes (26) side by side along the length direction of the pipes, a first stainless steel wire mesh matched with the shape of the sludge discharge pipes is arranged at an orifice, and the mesh size of the first stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding chamber; a sludge discharge groove (27) is formed in the lower side of the slope structure, the lower end of a sludge discharge pipe (26) is connected to the sludge discharge groove (27), the gradient of the bottom of the long side of the sludge discharge groove (27) is set to be 2% -3%, a second stainless steel wire mesh matched with the sludge discharge groove in shape is covered above the sludge discharge groove (27), and the mesh size of the second stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding cavity; mud discharging branch pipes (28) are reserved in the wetland side walls corresponding to the mud discharging grooves (27), and the outer ends of the mud discharging branch pipes (28) are connected with a mud discharging main pipe (29) together.\|	(CN113683197)\|Aiming at the problems in the prior art, the invention provides an artificial wetland ecological restoration process. In order to achieve the purpose, the invention is realized by the following technical scheme:\|The invention discloses an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system, which relates to the technical field of constructed wetland construction and comprises an aeration reoxygenation chamber, an enhanced decarbonization chamber, an enhanced nitrogen removal chamber, an enhanced phosphorus removal chamber, a sludge sedimentation tank and the like.\|The invention relates to the technical field of sewage treatment, in particular to an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system.\|	(CN113683197)\|AERATION REOXYGENATION CHAMBER(100,39)\|CONSTRUCTED WETLAND(100,20)\|PHOSPHORUS REMOVAL(100,12)\|NITROGEN(100,11)\|COMPOSITE FILLER(75,37)\|ENHANCED DECARBONIZATION CHAMBER(65,23)\|ENHANCED DENITRIFICATION CHAMBER(61,26)\|SLUDGE DISCHARGE PIPE(58,8)\|ENHANCED PHOSPHORUS REMOVAL CHAMBER(49,9)\|PHOSPHORUS REMOVAL CHAMBER(47,11)\|OBSERVATION CHAMBER(35,17)\|MICROORGANISM IMMOBILIZATION(35,8)\|MUD DISCHARGE(34,1)\|SLUDGE SEDIMENTATION TANK(33,9)\|ENHANCED DEPHOSPHORIZATION CHAMBER(31,16)\|SUSPENDED CERAMSITE(30,6)\|ARTIFICIAL WETLAND ECOLOGICAL RESTORATION(30,1)\|BRANCH PIPE(29,15)\|SLUDGE(28,28)\|AERATION REOXYGENATION CHAMBER BOTTOM(28,10)\|NITROGEN REMOVAL CHAMBER(27,3)\|ENHANCED NITROGEN REMOVAL CHAMBER(26,3)\|SLUDGE SETTLING TANK(25,13)\|DENITRIFICATION(21,2)\|ANTIBLOCKING CONSTRUCTED WETLAND(20,2)\|GRAVEL(19,10)\|BROKEN ROCK(19,7)\|SLUDGE DISCHARGE GROOVE(19,3)\|FILLER CENTRALIZATION(19,2)\|OVERFLOW PIPE(18,23)\|SUPERNATANT OUTLET(17,4)\|WATER INLET(16,22)\|AERATION(16,5)\|MUD SEDIMENTATION TANK(16,1)\|RESERVING WATER PIPE(15,11)\|CRUSHED STONE(15,5)\|ECOLOGICAL RESTORATION(15,1)\|SLOPE(13,12)\|EARTH FILTRATION(13,2)\|INSUFFICIENT DISSOLVED OXYGEN(13,1)\|STRICT EMISSION STANDARD(13,1)\|SLOPE STRUCTURE(12,6)\|GRADIENT(12,5)\|UPPER COVERING SOIL(12,2)\|COAL ASH(12,1)\|CONSTRUCTED WETLAND CONSTRUCTION(12,1)\|MUD(11,16)\|LIMESTONE(11,3)\|VOLCANIC ROCK(11,3)\|AERATION MAIN PIPE(11,2)\|BIOCHAR(11,2)\|SEPARATION NET(11,1)\|WATER DRAINAGE CHANNEL(10,3)\|DESIGNED ENHANCED DECARBONIZATION CHAMBER(10,2)\|ORIFICE(10,2)\|ARTIFICIAL WETLAND(9,6)\|REINFORCED DENITRIFICATION CHAMBER(9,6)\|POWER MUD(9,5)\|REINFORCED DEPHOSPHORIZATION CHAMBER(9,4)\|ZEOLITE(9,3)\|LAYOUT(9,1)\|DISTRIBUTION(8,2)\|OXYGEN DEMAND(8,1)\|SUBSURFACE FLOW CONSTRUCTED WETLAND(8,1)\|STAINLESS STEEL WIRE MESH(7,9)\|DRAINAGE CHANNEL(7,5)\|UPPER GRAVEL LAYER(7,5)\|SEWAGE TREATMENT(7,4)\|MUD PUMP(7,3)\|SLUDGE DISCHARGE VALVE(7,3)\|STRENGTHENING DECARBONIZATION CHAMBER(7,2)\|MINIMUM PARTICLE SIZE(6,5)\|AQUATIC PLANT(6,4)\|PURIFIED WATER COLLECTION(6,2)\|UNIT MODULE(6,2)\|DTG IMMOBILIZED MICROORGANISM(6,1)\|MESH SIZE(5,6)\|FILLER COMPOUND(5,5)\|INLET WATER(5,2)\|PURIFYING WATER QUALITY(5,2)\|REINFORCED DECARBONIZATION CHAMBER(5,2)\|SUBSURFACE FLOW(5,2)\|ACCUMULATED IMPURITY SLUDGE(5,1)\|AFFORESTATION VEGETATION(5,1)\|INTENSIFIED DECARBONIZATION CHAMBER(5,1)\|THREE LAYER NYLON NET(4,5)\|MUD OUTER END(4,3)\|SUPERNATANT DELIVERY PORT(4,2)\|GREEN VEGETATION(4,1)\|SLUDGE GATHERING TANK(4,1)\|WETLAND BLOCKING PHENOMENON(4,1)\|HIGH EFFICIENCY NITROGEN(3,3)\|INCLINED PLANE(3,3)\|MUD PIPE(3,3)\|LENGTH DIRECTION(3,2)\|REINFORCED PHOSPHORUS REMOVAL CHAMBER(3,2)\|SLUDGE SIDE(3,2)\|AERATION PIPELINE(3,1)\|AERATION ROLE(3,1)\|ENHANCED DENITRIFICATION(3,1)\|GATHERING MUD GROOVE(3,1)\|HIGH EFFICIENCY DENITRIFICATION(3,1)\|MICROBIAL DECOMPOSITION(3,1)\|SLUDGE SETTLING TANK LATERAL(3,1)\|SOIL TRIPLE SYNERGISTIC ACTION(3,1)\|TRANSPIRATION MOISTURE(3,1)\|WETLAND SLUDGE(3,1)\|OUTER END(2,6)\|COVER PLATE(2,3)\|WETLAND SIDE WALL(2,3)\|HEAVY METAL(2,2)\|POWER SLUDGE(2,2)\|CHAMBER TANK(2,1)\|DEPHOSPHORIZATION ARTIFICIAL WETLAND(2,1)\|GROUND COVER(2,1)\|INSULATION(2,1)\|MUD DISCHARGE MAIN PIPE(2,1)\|MUD VALVE(2,1)\|NUTRIENT ABSORPTION(2,1)\|NYLON NET LAYER(2,1)\|OBSERVATION ROOM(2,1)\|OVERFLOW TUBE(2,1)\|PLANT ROOT ADSORPTION(2,1)\|PLANT SHIELDING(2,1)\|PREBURIED MANY MUD(2,1)\|RESIDUE ACCUMULATION(2,1)\|RURAL SEWAGE TREATMENT(2,1)\|SEWAGE PLANT DEEP TREATMENT(2,1)\|SEWAGE TREATMENT DECENTRALIZATION(2,1)\|SLUDGE DISCHARGE MAIN PIPE(2,1)\|SLUDGE PUMP(2,1)\|SLUDGE SETTLING TANK OUTSIDE(2,1)\|SUBSTANCE SUSPENSION(2,1)\|UPPER STRATA EARTHING(2,1)\|WATER INLET INTERCOMMUNICATION(2,1)\|WETLAND PURIFICATION AREA(2,1)\|LONG SIDE(1,2)\|ANIMAL(1,1)\|APRON(1,1)\|ARTIFICIAL CONSTRUCTION MODE(1,1)\|ARTIFICIAL MEDIUM(1,1)\|ARTIFICIAL WETLAND DESIGN(1,1)\|DETENTION(1,1)\|DRILL WAY DEPARTMENT(1,1)\|	(CN113683197)\|1. An efficient nitrogen and phosphorus removal anti-blocking constructed wetland system is characterized by comprising an aeration reoxygenation chamber (1), an enhanced decarbonization chamber (2), an enhanced denitrification chamber (3) and an enhanced phosphorus removal chamber (4), wherein a water inlet channel (5) is arranged on the front side of the aeration reoxygenation chamber (1), an observation chamber (6) is arranged between the enhanced decarbonization chamber (2) and the enhanced denitrification chamber (3), and a water drainage channel (7) is arranged on the rear side of the enhanced phosphorus removal chamber (4);\|the water inlet channel (5) is communicated with the aeration reoxygenation chamber (1) through a first overflow pipe (9), a main pipe (10) and branch pipes are arranged below the aeration reoxygenation chamber (1), and the outer end of the main pipe (10) is connected with an aeration device;\|a first composite filler (12) is filled in the aeration reoxygenation chamber (1), the first composite filler (12) comprises at least two of large-particle-size crushed stone, gravel, volcanic rock and suspended ceramsite, and the suspended ceramsite contains immobilized microorganisms;\|the enhanced decarbonization chamber (2) is positioned at the rear side of the aeration reoxygenation chamber (1) and is communicated with the aeration reoxygenation chamber through a second overflow pipe (13), a second composite filler (14) is filled in the enhanced decarbonization chamber (2), and the second composite filler (14) comprises gravel, broken stone and limestone;\|the enhanced denitrification chamber (3) is positioned at the rear side of the observation chamber (6), a third overflow pipe (15) and a first reserved water pipe (16) are respectively arranged at two sides of the observation chamber (6), the third overflow pipe (15) is communicated with the enhanced decarbonization chamber (2) and the observation chamber (6), the first reserved water pipe (16) is arranged at the bottom and is communicated with the observation chamber (6) and the enhanced denitrification chamber (3); a third composite filler (17) is filled in the enhanced denitrification chamber (3), and the third composite filler (17) comprises gravel, biochar and broken stone;\|the enhanced phosphorus removal chamber (4) is positioned at the rear side of the enhanced nitrogen removal chamber (3), the enhanced phosphorus removal chamber (4) is communicated with the enhanced nitrogen removal chamber (3) through a fourth overflow pipe (18), a fourth composite filler (19) is filled in the enhanced phosphorus removal chamber, the fourth composite filler (19) comprises gravel, zeolite, coal ash and crushed stone, and the enhanced phosphorus removal chamber (4) is communicated with the drainage channel (7) through a second reserved water pipe (20) arranged at the bottom;\|the bottom of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced dephosphorization chamber (4) is of a slope structure, a plurality of sludge discharge pipes (26) are pre-buried at the bottoms of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced dephosphorization chamber (4), the sludge discharge pipes (26) are laid on the slope, a plurality of holes are formed in the sludge discharge pipes (26) side by side along the length direction of the pipes, a first stainless steel wire mesh matched with the shape of the sludge discharge pipes is arranged at an orifice, and the mesh size of the first stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding chamber; a sludge discharge groove (27) is formed in the lower side of the slope structure, the lower end of a sludge discharge pipe (26) is connected to the sludge discharge groove (27), the gradient of the bottom of the long side of the sludge discharge groove (27) is set to be 2% -3%, a second stainless steel wire mesh matched with the sludge discharge groove in shape is covered above the sludge discharge groove (27), and the mesh size of the second stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding cavity; mud discharging branch pipes (28) are reserved in the wetland side walls corresponding to the mud discharging grooves (27), and the outer ends of the mud discharging branch pipes (28) are connected with a mud discharging main pipe (29) together.\|2. The high-efficiency nitrogen and phosphorus removal anti-blocking constructed wetland system of claim 1, a water inlet (8) is arranged on one side of the water inlet channel (5), a sludge sedimentation tank (32) is arranged at the output end of the sludge discharge main pipe (29), a cover plate (33) is arranged at the top of the sludge sedimentation tank (32), a supernatant outlet (34) is arranged on the side part of the sludge sedimentation tank (32), the supernatant outlet (34) is communicated with the water inlet (8), a sludge gathering groove (35) is arranged in the middle of the bottom of the sludge settling tank (32), the bottoms of the sludge settling tank (32) at two sides of the sludge gathering groove (35) are inclined planes with certain gradient, one side close to the sludge gathering groove (35) is a low side, a mud pump (36) is arranged in the mud gathering groove (35), the mud pump (36) is connected with a power mud conveying pipe (37), and the output end of the power mud conveying pipe (37) extends to the outer side of the mud sedimentation tank (32).\|3. The efficient nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 2, wherein the slope of the slopes on two sides of the bottom of the sludge settling tank (32) is 2%.\|4. The high-efficiency nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, characterized in that a support (11) is laid under the aeration main pipe (10) and the branch pipes, and the end of the support (11) is fixedly connected to the bottom of the aeration reoxygenation chamber (1).\|5. The high-efficiency denitrification and dephosphorization anti-blocking constructed wetland system according to claim 1, wherein the immobilized microorganisms are preferably DTG immobilized microorganisms.\|6. The efficient nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, wherein the thicknesses of the first composite filler (12), the second composite filler (14), the third composite filler (17) and the fourth composite filler (19) are controlled to be 10-50 mm, a lower gravel layer (21) with the thickness of 60-100 mm is arranged at the bottom of each layer of composite filler, an upper gravel layer (22) with the thickness of 5-10 mm is arranged at the top of each layer of composite filler, a three-layer nylon net (23) is arranged at the top of the upper gravel layer (22), upper covering soil (24) is laid at the top of the three-layer nylon net (23), and greening vegetation (25) is arranged on the upper covering soil (24).\|7. The efficient nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, wherein the slope of the slope structures at the bottoms of the aeration reoxygenation chamber (1), the enhanced decarbonization chamber (2), the enhanced denitrification chamber (3) and the enhanced phosphorus removal chamber (4) is 2%.\|8. The denitrification and dephosphorization anti-blocking constructed wetland system according to claim 1, wherein the sludge discharge pipe (26) and the sludge discharge groove (27) are vertically connected in spatial position.\|9. The efficient nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, characterized in that sludge discharge valves (30) are independently arranged on the sludge discharge branch pipes (28), and a main valve (30) is arranged on the sludge discharge main pipe (29).\|10. The high-efficiency nitrogen and phosphorus removal anti-blocking constructed wetland system according to claim 1, characterized in that a separation net (38) is arranged above the water inlet channel (5), the observation chamber (6) and the water drainage channel (7).	(CN113683197)\|TECHNICAL FIELD\|[0001] The invention relates to the technical field of sewage treatment, in particular to an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system.\|BACKGROUND ART\|[0002] The artificial wetland is a technology for treating sewage and sludge by using the physical, chemical and biological triple synergistic action of soil, artificial medium, plants and microorganisms in the process of flowing along a certain direction by using sewage and sludge which are controllably dosed to the artificially constructed wetland from the artificially constructed and controlled-operation ground similar to the marshland. The action mechanism of the plant nutrient solution comprises the actions of adsorption, detention, filtration, oxidation reduction, precipitation, microbial decomposition, transformation, plant shielding, residue accumulation, transpiration moisture and nutrient absorption and various animals.\|[0003] However, the conventional subsurface flow constructed wetland has insufficient dissolved oxygen and the denitrification effect is difficult to meet the strict emission standard, so the current challenges are to effectively balance the oxygen demand and input in the artificial system under the condition of reducing the cost and how to design a system which can ensure the treatment efficiency and keep the system simple and economic in the aspects of layout, construction and maintenance. And because the suspended substances in the sewage are intercepted and the biological membranes on the surface of the substrate are accumulated and shed, the artificial wetland is easy to block in the actual operation.\|DISCLOSURE\|Disclosure of Invention\|[0004] Aiming at the problems in the prior art, the invention provides an artificial wetland ecological restoration process.\|[0005] In order to achieve the purpose, the invention is realized by the following technical scheme:\|[0006] an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system comprises an aeration reoxygenation chamber, a reinforced decarbonization chamber, a reinforced denitrification chamber and a reinforced phosphorus removal chamber, wherein a water inlet channel is arranged on the front side of the aeration reoxygenation chamber, an observation chamber is arranged between the reinforced decarbonization chamber and the reinforced denitrification chamber, and a water drainage channel is arranged on the rear side of the reinforced phosphorus removal chamber; the water inlet channel is communicated with the aeration reoxygenation chamber through a first overflow pipe, a main pipe and a branch pipe are arranged below the aeration reoxygenation chamber, and the outer end of the main pipe is connected with an aeration device; filling a first composite filler in the aeration reoxygenation chamber, wherein the first composite filler comprises at least two of large-particle-size crushed stone, gravel, volcanic rock and suspended ceramsite, and the suspended ceramsite contains immobilized microorganisms; the strengthening decarbonization chamber is positioned at the rear side of the aeration reoxygenation chamber and is communicated with the aeration reoxygenation chamber through a second overflow pipe, and second composite fillers are filled in the strengthening decarbonization chamber and comprise gravels, broken stones and limestone; the enhanced denitrification chamber is positioned at the rear side of the observation chamber, a third overflow pipe and a first reserved water pipe are respectively arranged at two sides of the observation chamber, the third overflow pipe is communicated with the enhanced decarbonization chamber and the observation chamber, and the first reserved water pipe is arranged at the bottom and is communicated with the observation chamber and the enhanced denitrification chamber; a third composite filler is filled in the enhanced denitrification chamber, and comprises gravels, charcoal and broken stones; the reinforced dephosphorization chamber is positioned at the rear side of the reinforced denitrification chamber, the reinforced dephosphorization chamber is communicated with the reinforced denitrification chamber through a fourth overflow pipe, a fourth composite filler is filled in the reinforced dephosphorization chamber, the fourth composite filler comprises gravel, zeolite, fly ash and broken stone, and the reinforced dephosphorization chamber is communicated with the drainage channel through a second reserved water pipe arranged at the bottom;\|[0007] the bottom of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber is of a slope structure, a plurality of sludge discharge pipes are pre-buried at the bottoms of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber and laid on the slope, a plurality of holes are arranged in the sludge discharge pipes side by side along the length direction of the pipes, a first stainless steel wire mesh matched with the shape of the first stainless steel wire mesh is arranged at an orifice, and the mesh size of the first stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding chamber; a mud discharging groove is formed in the lower side of the slope structure, the lower end of the mud discharging pipe is connected to the mud discharging groove, the gradient of the bottom of the long side of the mud discharging groove is set to be 2% -3%, a second stainless steel wire mesh matched with the shape of the mud discharging groove is covered above the mud discharging groove, and the mesh size of the second stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding cavity; mud discharge branch pipes are reserved in the wetland side walls corresponding to the mud discharge grooves, and the outer ends of the mud discharge branch pipes are connected with a mud discharge main pipe.\|[0008] Further, a water inlet has been seted up on one side of the above-mentioned inlet channel, be equipped with sludge settling tank at the mud main pipe output of arranging, the sludge settling tank top is equipped with the apron, sludge settling tank lateral part is equipped with the supernatant delivery port, supernatant delivery port and water inlet intercommunication, bottom intermediate position at sludge settling tank has been seted up and has been gathered mud groove, gather the inclined plane of sludge settling tank bottom for having certain slope on mud groove both sides, be close to the low side that is of gathering mud groove one side, be equipped with the slush pump in gathering mud groove, the slush pump is connected with power mud conveying pipe, the output of power mud conveying pipe extends to the sludge settling tank outside.\|[0009] Furthermore, a bracket is laid under the aeration main pipe and the branch pipe, and the end part of the bracket is fixedly connected with the bottom of the aeration reoxygenation chamber.\|[0010] Preferably, the immobilized microorganism is a DTG immobilized microorganism.\|[0011] Further, the thickness control of above-mentioned first compound filler, the compound filler of second, the compound filler of third and the compound filler of fourth is at 10 ~ 50mm, is equipped with the lower gravel layer that thickness is 60 ~ 100mm in the bottom of each layer compound filler, is equipped with the last gravel layer that thickness is 5 ~ 10mm at the top of each layer compound filler, is equipped with the three-layer nylon net at last gravel layer top, has laid the upper earthing at the three-layer nylon net top, is provided with the afforestation vegetation on the earthing of upper strata.\|[0012] Furthermore, the slope of the slope structures at the bottoms of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber is 2 percent.\|[0013] Furthermore, a sludge discharge valve is independently arranged on each sludge discharge branch pipe, and a main sludge discharge pipe is provided with a main valve.\|[0014] The artificial wetland process at least comprises the following beneficial effects:\|[0015] the constructed wetland system adopts an artificial construction mode to construct a pool body, which comprises an aeration reoxygenation chamber, an enhanced decarbonization chamber, an enhanced denitrification chamber, an enhanced dephosphorization chamber, a sludge sedimentation tank and the like. The water inlet channel mainly has the functions of uniformly distributing water and collecting purified water; the aeration reoxygenation chamber is a main body unit for purifying water quality, mainly comprising an aeration device, a composite filler and plants, and when polluted water flows through the unit module, the water quality can be purified by virtue of the composite filler, soil filtration, aquatic plants, efficient microorganism activities and the like; the composite filler can select different centralized fillers according to the quality of inlet water and the water quality target required to be achieved, so that the designed enhanced decarbonization chamber, enhanced denitrification chamber, enhanced dephosphorization chamber and sludge sedimentation tank can effectively remove nitrogen, phosphorus, heavy metals, impurity sludge and the like in the water body, and the accumulated impurity sludge or suspended matters are collected into the sedimentation tank through the inclination, sludge discharge pipes, sludge discharge grooves, sludge discharge branches/main pipes and the like arranged along the bottom of the tank body of each chamber and then discharged out through the slurry pump.\|DRAWINGS DESCRIPTION\|[0016] The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:\|[0017] fig. 1 is a plan layout view of an artificial wetland system of the present invention;\|[0018] FIG. 2 is a schematic diagram of the arrangement structure of a sludge discharge pipe at the bottom of the constructed wetland system of the invention;\|[0019] FIG. 3 is a cross-sectional view taken at A-A of FIG. 1;\|[0020] FIG. 4 is a cross-sectional view at B-B in FIG. 1 (intended to illustrate the structural level of the wetland from bottom to top);\|[0021] FIG. 5 is a cross-sectional view taken at C-C of FIG. 1;\|[0022] labeled as: 1. an aeration reoxygenation chamber; 2. an intensified decarbonization chamber; 3. a reinforced denitrification chamber; 4. strengthening a dephosphorization chamber; 5. a water inlet channel; 6. an observation room; 7. a drainage channel; 8. a water inlet; 9. a first overflow pipe; 10. a main pipe; 11. a support; 12. a first composite filler; 13. a second overflow tube; 14. a second composite filler; 15. a third overflow pipe; 16. a first reserved water pipe; 17. a third composite filler; 18. a fourth overflow pipe; 19. a fourth composite filler; 20. a second reserved water pipe; 21. a lower gravel layer; 22. an upper gravel layer; 23. three layers of nylon nets; 24. covering soil on the upper layer; 25. greening vegetation; 26. a sludge discharge pipe; 27. a sludge discharge groove; 28. a sludge discharge branch pipe; 29. a sludge discharge main pipe; 30. a mud valve; 31. a main valve; 32. a sludge sedimentation tank; 33. a cover plate; 34. a water outlet; 35. a sludge gathering tank; 36. a slurry pump; 37. a power mud conveying pipe; 38. and (4) isolating nets.\|INVENTION MODE\|Detailed Description\|[0023] In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention.\|[0024] Referring to fig. 1-3, the present invention provides a modular combined enhanced denitrification and dephosphorization artificial wetland process, i.e., a multi-stage novel subsurface flow artificial wetland system. Specifically, the system mainly comprises the following four processing units: an aeration reoxygenation chamber 1 (wetland purification area), an enhanced decarbonization chamber 2, an enhanced denitrification chamber 3 and an enhanced dephosphorization chamber 4, wherein a water inlet channel 5 (water collecting area) is arranged in front of the aeration reoxygenation chamber 1, an observation chamber 6 is arranged between the enhanced decarbonization chamber 2 and the enhanced denitrification chamber 3, and a water discharge channel 7 is arranged behind the enhanced dephosphorization chamber 4.\|[0025] Wherein, a water inlet 8 is arranged on one side of the water inlet channel 5, the water inlet channel 5 is communicated with the aeration reoxygenation chamber 1 through a first overflow pipe 9 arranged above, a main pipe 10 and a branch pipe (not shown) are arranged below the aeration reoxygenation chamber 1, the outer end of the main pipe 10 is connected with an aeration device (not shown), and the main pipe 10 and the branch pipe are arranged to play an aeration role in the water body of the aeration reoxygenation chamber 1. Furthermore, a support 11 is laid under the aeration main pipe 10 and the branch pipes, which mainly plays a role of supporting the aeration pipeline, and the end part of the support 11 is fixedly connected to the bottom of the aeration reoxygenation chamber 1.\|[0026] Referring to fig. 3 again, the aeration reoxygenation chamber 1 is filled with a first composite filler 12, and the first composite filler 12 is two or more of crushed stone with large particle size, gravel, volcanic rock and suspended ceramsite, wherein the suspended ceramsite contains immobilized microorganisms, and the immobilized microorganisms are preferably DTG immobilized microorganisms.\|[0027] In light of the above, the enhanced decarbonization chamber 2 is located behind the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2 is communicated with the aeration reoxygenation chamber 1 through a second overflow pipe 13 arranged above, and the enhanced decarbonization chamber 2 is filled with a second composite filler 14, wherein the second composite filler 14 mainly comprises gravel, broken stone and limestone.\|[0028] The enhanced denitrification chamber 3 is positioned behind the observation chamber 6, a third overflow pipe 15 and a first reserved water pipe 16 are respectively arranged on two sides of the observation chamber 6, the third overflow pipe 15 is communicated with the enhanced decarbonization chamber 2 and the observation chamber 6, and the first reserved water pipe 16 is arranged at the bottom and is communicated with the observation chamber 6 and the enhanced denitrification chamber 3; further, the reinforced denitrification chamber 3 is filled with a third composite filler 17, and the third composite filler 17 mainly comprises gravel, biochar and crushed stone.\|[0029] The enhanced dephosphorization chamber 4 is positioned behind the enhanced denitrification chamber 3, the enhanced dephosphorization chamber 4 is communicated with the enhanced denitrification chamber 3 through a fourth overflow pipe 18 arranged above, and a fourth composite filler 19 is filled in the enhanced dephosphorization chamber, wherein the fourth composite filler 19 mainly comprises gravel, zeolite, fly ash and broken stone. The enhanced phosphorus removal chamber 4 is communicated with the drainage channel 7 through a second reserved water pipe 20 arranged at the bottom.\|[0030] Referring to fig. 4, preferably, aquatic plants are planted above the first composite filler 12, the second composite filler 14, the third composite filler 17 and the fourth composite filler 19, so as to provide plant root adsorption for purifying the water in each chamber; preferably, the thicknesses of the first composite filler 12, the second composite filler 14, the third composite filler 17 and the fourth composite filler 19 are 10-50 mm, the bottom of each layer of composite filler is provided with a lower gravel layer 21 with the thickness of 60-100 mm, the top of each layer of composite filler is provided with an upper gravel layer 22 with the thickness of 5-10 mm, the top of the upper gravel layer 22 is provided with a three-layer nylon net 23, the top of the three-layer nylon net 23 is paved with upper-layer soil cover 24, and greening vegetation 25 (namely aquatic plants) is paved on the upper-layer soil cover 24.\|[0031] Referring to fig. 2 and 3 again, the bottoms of the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4 are slope structures with slopes of 2%, that is, the bottom of the water inlet side and the height of the water outlet side [ slope 2% ((height difference/horizontal distance between the water outlet side and the water inlet side) x 100%). Simultaneously at the pre-buried many mud pipes 26 that are provided with of above-mentioned each cavity bottom, furtherly, mud pipe 26 lays on the slope, and mud pipe 26 both ends have the slope equally, have seted up a plurality of holes side by side along the tube length direction at mud pipe 26 to be equipped with rather than shape assorted first stainless steel net (not shown) in drill way department, the mesh size of first stainless steel net should be less than the minimum particle diameter that corresponds compound filler in the cavity.\|[0032] In the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4 are all provided with the sludge discharge groove 27 at the lower side of the slope, the lower end of the sludge discharge pipe 26 is connected to the sludge discharge groove 27, the sludge discharge pipe 26 and the sludge discharge groove 27 are in a vertical connection state in the spatial position, the slope of the bottom of the long edge of the sludge discharge groove 27 is set to be 2% -3%, the sludge discharge groove 27 is covered with a second stainless steel wire net (not shown) matched with the shape of the sludge discharge pipe, and the mesh size of the second stainless steel wire net is smaller than the minimum particle size of the composite filler in the corresponding chamber. Mud discharging branch pipes 28 are reserved in the wetland side walls corresponding to the mud discharging grooves 27, the outer ends of the mud discharging branch pipes 28 are connected with a mud discharging main pipe 29, mud discharging valves 30 are independently arranged on the mud discharging branch pipes 28, and a main valve 31 is arranged on the mud discharging main pipe 29.\|[0033] Referring to fig. 5, a sludge settling tank 32 is disposed at an output end of the main sludge discharge pipe 29, a cover plate 33 is disposed at a top of the sludge settling tank 32, a supernatant outlet 34 is disposed at a side portion of the sludge settling tank 32, the supernatant outlet 34 is communicated with the water inlet 8 on the water inlet channel 5, a sludge collecting groove 35 is disposed at a middle position of a bottom of the sludge settling tank 32, the bottoms of the sludge settling tanks 32 on two sides of the sludge collecting groove 35 are inclined planes with a certain gradient (gradient is 2%), and a lower side is disposed at a side close to the sludge collecting groove 35, so that sludge can be automatically collected into the sludge collecting groove 35 under the action of gravity, a sludge pump 36 is fixedly disposed in the sludge collecting groove 35, the sludge pump 36 is connected with a power sludge conveying pipe 37, and the power sludge conveying pipe 37 penetrates through the sludge settling tank 32 and extends to the outside.\|[0034] After the constructed wetland system disclosed by the invention normally operates, the whole wetland system or a certain single module (namely four units of the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4) can be regularly controlled to carry out wetland sludge discharge operation through the sludge discharge valve 30 and the main valve 31, and water in the drainage channel 7 can be used for recharging back to carry out back flushing, so that the sludge discharge operation is carried out more efficiently, and the wetland blocking phenomenon is improved. The discharged sludge enters the sludge sedimentation tank 32 for sedimentation and can be discharged by a mud pump 36, and the supernatant liquid of the sludge sedimentation tank 32 flows back to the water inlet channel 5 through the water outlet 34.\|[0035] The invention can be suitable for all artificial wetland designs, such as tail water deep treatment of sewage plants, decentralized sewage treatment (such as rural sewage treatment) and the like; in practice, the pipe diameters and the numbers of the overflow pipes (the first overflow pipe 9, the second overflow pipe 13, the third overflow pipe 15, and the fourth overflow pipe 18) at the respective positions can be adjusted and changed according to actual needs, and a partition net 38 is provided above the inlet channel 5, the observation chamber 6, and the drain channel 7.\|[0036] Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.	(CN113683197)\|TECHNICAL FIELD\|[0001] The invention relates to the technical field of sewage treatment, in particular to an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system.\|BACKGROUND ART\|[0002] The artificial wetland is a technology for treating sewage and sludge by using the physical, chemical and biological triple synergistic action of soil, artificial medium, plants and microorganisms in the process of flowing along a certain direction by using sewage and sludge which are controllably dosed to the artificially constructed wetland from the artificially constructed and controlled-operation ground similar to the marshland. The action mechanism of the plant nutrient solution comprises the actions of adsorption, detention, filtration, oxidation reduction, precipitation, microbial decomposition, transformation, plant shielding, residue accumulation, transpiration moisture and nutrient absorption and various animals.\|[0003] However, the conventional subsurface flow constructed wetland has insufficient dissolved oxygen and the denitrification effect is difficult to meet the strict emission standard, so the current challenges are to effectively balance the oxygen demand and input in the artificial system under the condition of reducing the cost and how to design a system which can ensure the treatment efficiency and keep the system simple and economic in the aspects of layout, construction and maintenance. And because the suspended substances in the sewage are intercepted and the biological membranes on the surface of the substrate are accumulated and shed, the artificial wetland is easy to block in the actual operation.\|DISCLOSURE\|Disclosure of Invention\|[0004] Aiming at the problems in the prior art, the invention provides an artificial wetland ecological restoration process.\|[0005] In order to achieve the purpose, the invention is realized by the following technical scheme:\|[0006] an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system comprises an aeration reoxygenation chamber, a reinforced decarbonization chamber, a reinforced denitrification chamber and a reinforced phosphorus removal chamber, wherein a water inlet channel is arranged on the front side of the aeration reoxygenation chamber, an observation chamber is arranged between the reinforced decarbonization chamber and the reinforced denitrification chamber, and a water drainage channel is arranged on the rear side of the reinforced phosphorus removal chamber; the water inlet channel is communicated with the aeration reoxygenation chamber through a first overflow pipe, a main pipe and a branch pipe are arranged below the aeration reoxygenation chamber, and the outer end of the main pipe is connected with an aeration device; filling a first composite filler in the aeration reoxygenation chamber, wherein the first composite filler comprises at least two of large-particle-size crushed stone, gravel, volcanic rock and suspended ceramsite, and the suspended ceramsite contains immobilized microorganisms; the strengthening decarbonization chamber is positioned at the rear side of the aeration reoxygenation chamber and is communicated with the aeration reoxygenation chamber through a second overflow pipe, and second composite fillers are filled in the strengthening decarbonization chamber and comprise gravels, broken stones and limestone; the enhanced denitrification chamber is positioned at the rear side of the observation chamber, a third overflow pipe and a first reserved water pipe are respectively arranged at two sides of the observation chamber, the third overflow pipe is communicated with the enhanced decarbonization chamber and the observation chamber, and the first reserved water pipe is arranged at the bottom and is communicated with the observation chamber and the enhanced denitrification chamber; a third composite filler is filled in the enhanced denitrification chamber, and comprises gravels, charcoal and broken stones; the reinforced dephosphorization chamber is positioned at the rear side of the reinforced denitrification chamber, the reinforced dephosphorization chamber is communicated with the reinforced denitrification chamber through a fourth overflow pipe, a fourth composite filler is filled in the reinforced dephosphorization chamber, the fourth composite filler comprises gravel, zeolite, fly ash and broken stone, and the reinforced dephosphorization chamber is communicated with the drainage channel through a second reserved water pipe arranged at the bottom;\|[0007] the bottom of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber is of a slope structure, a plurality of sludge discharge pipes are pre-buried at the bottoms of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber and laid on the slope, a plurality of holes are arranged in the sludge discharge pipes side by side along the length direction of the pipes, a first stainless steel wire mesh matched with the shape of the first stainless steel wire mesh is arranged at an orifice, and the mesh size of the first stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding chamber; a mud discharging groove is formed in the lower side of the slope structure, the lower end of the mud discharging pipe is connected to the mud discharging groove, the gradient of the bottom of the long side of the mud discharging groove is set to be 2% -3%, a second stainless steel wire mesh matched with the shape of the mud discharging groove is covered above the mud discharging groove, and the mesh size of the second stainless steel wire mesh is smaller than the minimum particle size of the composite filler in the corresponding cavity; mud discharge branch pipes are reserved in the wetland side walls corresponding to the mud discharge grooves, and the outer ends of the mud discharge branch pipes are connected with a mud discharge main pipe.\|[0008] Further, a water inlet has been seted up on one side of the above-mentioned inlet channel, be equipped with sludge settling tank at the mud main pipe output of arranging, the sludge settling tank top is equipped with the apron, sludge settling tank lateral part is equipped with the supernatant delivery port, supernatant delivery port and water inlet intercommunication, bottom intermediate position at sludge settling tank has been seted up and has been gathered mud groove, gather the inclined plane of sludge settling tank bottom for having certain slope on mud groove both sides, be close to the low side that is of gathering mud groove one side, be equipped with the slush pump in gathering mud groove, the slush pump is connected with power mud conveying pipe, the output of power mud conveying pipe extends to the sludge settling tank outside.\|[0009] Furthermore, a bracket is laid under the aeration main pipe and the branch pipe, and the end part of the bracket is fixedly connected with the bottom of the aeration reoxygenation chamber.\|[0010] Preferably, the immobilized microorganism is a DTG immobilized microorganism.\|[0011] Further, the thickness control of above-mentioned first compound filler, the compound filler of second, the compound filler of third and the compound filler of fourth is at 10 ~ 50mm, is equipped with the lower gravel layer that thickness is 60 ~ 100mm in the bottom of each layer compound filler, is equipped with the last gravel layer that thickness is 5 ~ 10mm at the top of each layer compound filler, is equipped with the three-layer nylon net at last gravel layer top, has laid the upper earthing at the three-layer nylon net top, is provided with the afforestation vegetation on the earthing of upper strata.\|[0012] Furthermore, the slope of the slope structures at the bottoms of the aeration reoxygenation chamber, the enhanced decarbonization chamber, the enhanced denitrification chamber and the enhanced dephosphorization chamber is 2 percent.\|[0013] Furthermore, a sludge discharge valve is independently arranged on each sludge discharge branch pipe, and a main sludge discharge pipe is provided with a main valve.\|[0014] The artificial wetland process at least comprises the following beneficial effects:\|[0015] the constructed wetland system adopts an artificial construction mode to construct a pool body, which comprises an aeration reoxygenation chamber, an enhanced decarbonization chamber, an enhanced denitrification chamber, an enhanced dephosphorization chamber, a sludge sedimentation tank and the like. The water inlet channel mainly has the functions of uniformly distributing water and collecting purified water; the aeration reoxygenation chamber is a main body unit for purifying water quality, mainly comprising an aeration device, a composite filler and plants, and when polluted water flows through the unit module, the water quality can be purified by virtue of the composite filler, soil filtration, aquatic plants, efficient microorganism activities and the like; the composite filler can select different centralized fillers according to the quality of inlet water and the water quality target required to be achieved, so that the designed enhanced decarbonization chamber, enhanced denitrification chamber, enhanced dephosphorization chamber and sludge sedimentation tank can effectively remove nitrogen, phosphorus, heavy metals, impurity sludge and the like in the water body, and the accumulated impurity sludge or suspended matters are collected into the sedimentation tank through the inclination, sludge discharge pipes, sludge discharge grooves, sludge discharge branches/main pipes and the like arranged along the bottom of the tank body of each chamber and then discharged out through the slurry pump.\|DRAWINGS DESCRIPTION\|[0016] The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:\|[0017] fig. 1 is a plan layout view of an artificial wetland system of the present invention;\|[0018] FIG. 2 is a schematic diagram of the arrangement structure of a sludge discharge pipe at the bottom of the constructed wetland system of the invention;\|[0019] FIG. 3 is a cross-sectional view taken at A-A of FIG. 1;\|[0020] FIG. 4 is a cross-sectional view at B-B in FIG. 1 (intended to illustrate the structural level of the wetland from bottom to top);\|[0021] FIG. 5 is a cross-sectional view taken at C-C of FIG. 1;\|[0022] labeled as: 1. an aeration reoxygenation chamber; 2. an intensified decarbonization chamber; 3. a reinforced denitrification chamber; 4. strengthening a dephosphorization chamber; 5. a water inlet channel; 6. an observation room; 7. a drainage channel; 8. a water inlet; 9. a first overflow pipe; 10. a main pipe; 11. a support; 12. a first composite filler; 13. a second overflow tube; 14. a second composite filler; 15. a third overflow pipe; 16. a first reserved water pipe; 17. a third composite filler; 18. a fourth overflow pipe; 19. a fourth composite filler; 20. a second reserved water pipe; 21. a lower gravel layer; 22. an upper gravel layer; 23. three layers of nylon nets; 24. covering soil on the upper layer; 25. greening vegetation; 26. a sludge discharge pipe; 27. a sludge discharge groove; 28. a sludge discharge branch pipe; 29. a sludge discharge main pipe; 30. a mud valve; 31. a main valve; 32. a sludge sedimentation tank; 33. a cover plate; 34. a water outlet; 35. a sludge gathering tank; 36. a slurry pump; 37. a power mud conveying pipe; 38. and (4) isolating nets.\|INVENTION MODE\|Detailed Description\|[0023] In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention.\|[0024] Referring to fig. 1-3, the present invention provides a modular combined enhanced denitrification and dephosphorization artificial wetland process, i.e., a multi-stage novel subsurface flow artificial wetland system. Specifically, the system mainly comprises the following four processing units: an aeration reoxygenation chamber 1 (wetland purification area), an enhanced decarbonization chamber 2, an enhanced denitrification chamber 3 and an enhanced dephosphorization chamber 4, wherein a water inlet channel 5 (water collecting area) is arranged in front of the aeration reoxygenation chamber 1, an observation chamber 6 is arranged between the enhanced decarbonization chamber 2 and the enhanced denitrification chamber 3, and a water discharge channel 7 is arranged behind the enhanced dephosphorization chamber 4.\|[0025] Wherein, a water inlet 8 is arranged on one side of the water inlet channel 5, the water inlet channel 5 is communicated with the aeration reoxygenation chamber 1 through a first overflow pipe 9 arranged above, a main pipe 10 and a branch pipe (not shown) are arranged below the aeration reoxygenation chamber 1, the outer end of the main pipe 10 is connected with an aeration device (not shown), and the main pipe 10 and the branch pipe are arranged to play an aeration role in the water body of the aeration reoxygenation chamber 1. Furthermore, a support 11 is laid under the aeration main pipe 10 and the branch pipes, which mainly plays a role of supporting the aeration pipeline, and the end part of the support 11 is fixedly connected to the bottom of the aeration reoxygenation chamber 1.\|[0026] Referring to fig. 3 again, the aeration reoxygenation chamber 1 is filled with a first composite filler 12, and the first composite filler 12 is two or more of crushed stone with large particle size, gravel, volcanic rock and suspended ceramsite, wherein the suspended ceramsite contains immobilized microorganisms, and the immobilized microorganisms are preferably DTG immobilized microorganisms.\|[0027] In light of the above, the enhanced decarbonization chamber 2 is located behind the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2 is communicated with the aeration reoxygenation chamber 1 through a second overflow pipe 13 arranged above, and the enhanced decarbonization chamber 2 is filled with a second composite filler 14, wherein the second composite filler 14 mainly comprises gravel, broken stone and limestone.\|[0028] The enhanced denitrification chamber 3 is positioned behind the observation chamber 6, a third overflow pipe 15 and a first reserved water pipe 16 are respectively arranged on two sides of the observation chamber 6, the third overflow pipe 15 is communicated with the enhanced decarbonization chamber 2 and the observation chamber 6, and the first reserved water pipe 16 is arranged at the bottom and is communicated with the observation chamber 6 and the enhanced denitrification chamber 3; further, the reinforced denitrification chamber 3 is filled with a third composite filler 17, and the third composite filler 17 mainly comprises gravel, biochar and crushed stone.\|[0029] The enhanced dephosphorization chamber 4 is positioned behind the enhanced denitrification chamber 3, the enhanced dephosphorization chamber 4 is communicated with the enhanced denitrification chamber 3 through a fourth overflow pipe 18 arranged above, and a fourth composite filler 19 is filled in the enhanced dephosphorization chamber, wherein the fourth composite filler 19 mainly comprises gravel, zeolite, fly ash and broken stone. The enhanced phosphorus removal chamber 4 is communicated with the drainage channel 7 through a second reserved water pipe 20 arranged at the bottom.\|[0030] Referring to fig. 4, preferably, aquatic plants are planted above the first composite filler 12, the second composite filler 14, the third composite filler 17 and the fourth composite filler 19, so as to provide plant root adsorption for purifying the water in each chamber; preferably, the thicknesses of the first composite filler 12, the second composite filler 14, the third composite filler 17 and the fourth composite filler 19 are 10-50 mm, the bottom of each layer of composite filler is provided with a lower gravel layer 21 with the thickness of 60-100 mm, the top of each layer of composite filler is provided with an upper gravel layer 22 with the thickness of 5-10 mm, the top of the upper gravel layer 22 is provided with a three-layer nylon net 23, the top of the three-layer nylon net 23 is paved with upper-layer soil cover 24, and greening vegetation 25 (namely aquatic plants) is paved on the upper-layer soil cover 24.\|[0031] Referring to fig. 2 and 3 again, the bottoms of the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4 are slope structures with slopes of 2%, that is, the bottom of the water inlet side and the height of the water outlet side [ slope 2% ((height difference/horizontal distance between the water outlet side and the water inlet side) x 100%). Simultaneously at the pre-buried many mud pipes 26 that are provided with of above-mentioned each cavity bottom, furtherly, mud pipe 26 lays on the slope, and mud pipe 26 both ends have the slope equally, have seted up a plurality of holes side by side along the tube length direction at mud pipe 26 to be equipped with rather than shape assorted first stainless steel net (not shown) in drill way department, the mesh size of first stainless steel net should be less than the minimum particle diameter that corresponds compound filler in the cavity.\|[0032] In the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4 are all provided with the sludge discharge groove 27 at the lower side of the slope, the lower end of the sludge discharge pipe 26 is connected to the sludge discharge groove 27, the sludge discharge pipe 26 and the sludge discharge groove 27 are in a vertical connection state in the spatial position, the slope of the bottom of the long edge of the sludge discharge groove 27 is set to be 2% -3%, the sludge discharge groove 27 is covered with a second stainless steel wire net (not shown) matched with the shape of the sludge discharge pipe, and the mesh size of the second stainless steel wire net is smaller than the minimum particle size of the composite filler in the corresponding chamber. Mud discharging branch pipes 28 are reserved in the wetland side walls corresponding to the mud discharging grooves 27, the outer ends of the mud discharging branch pipes 28 are connected with a mud discharging main pipe 29, mud discharging valves 30 are independently arranged on the mud discharging branch pipes 28, and a main valve 31 is arranged on the mud discharging main pipe 29.\|[0033] Referring to fig. 5, a sludge settling tank 32 is disposed at an output end of the main sludge discharge pipe 29, a cover plate 33 is disposed at a top of the sludge settling tank 32, a supernatant outlet 34 is disposed at a side portion of the sludge settling tank 32, the supernatant outlet 34 is communicated with the water inlet 8 on the water inlet channel 5, a sludge collecting groove 35 is disposed at a middle position of a bottom of the sludge settling tank 32, the bottoms of the sludge settling tanks 32 on two sides of the sludge collecting groove 35 are inclined planes with a certain gradient (gradient is 2%), and a lower side is disposed at a side close to the sludge collecting groove 35, so that sludge can be automatically collected into the sludge collecting groove 35 under the action of gravity, a sludge pump 36 is fixedly disposed in the sludge collecting groove 35, the sludge pump 36 is connected with a power sludge conveying pipe 37, and the power sludge conveying pipe 37 penetrates through the sludge settling tank 32 and extends to the outside.\|[0034] After the constructed wetland system disclosed by the invention normally operates, the whole wetland system or a certain single module (namely four units of the aeration reoxygenation chamber 1, the enhanced decarbonization chamber 2, the enhanced denitrification chamber 3 and the enhanced dephosphorization chamber 4) can be regularly controlled to carry out wetland sludge discharge operation through the sludge discharge valve 30 and the main valve 31, and water in the drainage channel 7 can be used for recharging back to carry out back flushing, so that the sludge discharge operation is carried out more efficiently, and the wetland blocking phenomenon is improved. The discharged sludge enters the sludge sedimentation tank 32 for sedimentation and can be discharged by a mud pump 36, and the supernatant liquid of the sludge sedimentation tank 32 flows back to the water inlet channel 5 through the water outlet 34.\|[0035] The invention can be suitable for all artificial wetland designs, such as tail water deep treatment of sewage plants, decentralized sewage treatment (such as rural sewage treatment) and the like; in practice, the pipe diameters and the numbers of the overflow pipes (the first overflow pipe 9, the second overflow pipe 13, the third overflow pipe 15, and the fourth overflow pipe 18) at the respective positions can be adjusted and changed according to actual needs, and a partition net 38 is provided above the inlet channel 5, the observation chamber 6, and the drain channel 7.\|[0036] Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.	Family Number\|(97182255)\|97182255\|Abstract\|(CN113683197 A)\|The invention discloses an efficient nitrogen and phosphorus removal anti - blocking constructed wetland system , and relates to the technical field of constructed wetland construction . The system comprises an aeration reoxygenation chamber , an enhanced carbon removal chamber , an enhanced nitrogen removal chamber , an enhanced phosphorus removal chamber , a sludge sedimentation tank and the like . A water inlet channel is mainly used for uniformly distributing water and collecting purified water . The aeration reoxygenation chamber is a main body unit for water quality purification and mainly comprises an aeration device , composite filler and plants , and when a polluted water body flows through the unit module , the water quality can be purified by virtue of the composite filler , soil filtration , and activities of aquatic plants , high - efficiency microorganisms and the like . According to the water quality of inlet water and the water quality target needing to be achieved , different concentrated and matched fillers can be selected , so that the enhanced carbon removal chamber , the enhanced nitrogen removal chamber , the enhanced phosphorus removal chamber and the sludge sedimentation tank which are designed and obtained can effectively remove nitrogen , phosphorus , heavy metal , impurity sludge and the like in the water body . \|Independent Claims\|(CN113683197 A)\|( . . . ) a first composite filler ( 12 ) is filled in the aeration reoxygenation chamber ( 1 ) , the first composite filler ( 12 ) comprises at least two of large - particle - size crushed stone , gravel , volcanic rock and suspended ceramsite , and the suspended ceramsite contains immobilized microorganisms ; ( . . . ) \|	Environmental technology	C02F-001/00/1\|C02F-001/52\|C02F-003/10\|C02F-003/10/7\|C02F-003/10/8\|C02F-003/32\|C02F-009/00\|C02F-2001/007\|C02F-2003/001\|C02F-2101/105\|C02F-2101/20\|C02F-2209/22		C02F-001/00/1\|C02F-001/52\|C02F-003/10\|C02F-003/10/7\|C02F-003/10/8\|C02F-003/32\|C02F-009/00\|C02F-2001/007\|C02F-2003/001\|C02F-2101/105\|C02F-2101/20\|C02F-2209/22	C02F-003/32\|C02F-009/14\|C02F-101/10\|C02F-101/20	C02F-003/32\|C02F-009/14\|C02F-101/10\|C02F-101/20			CN114804550B	CN114804550B 101123923 WHO=Examiner SELF=N	CN110294531\|CN107662979\|CN103819004\|CN103739081\|CN105967334\|KR100631373	CN110294531 86184402 WHO=Examiner SELF=N CAT=Y\|CN107662979 78700132 WHO=Examiner SELF=N CAT=Y\|CN103819004 66109297 WHO=Examiner SELF=N CAT=Y\|CN103739081 65358640 WHO=Examiner SELF=N CAT=Y\|CN105967334 74265238 WHO=Examiner SELF=N CAT=A\|KR100631373 33903977 WHO=Examiner SELF=N CAT=A		KR100631373; CN103739081; CN103819004; CN105967334; CN107662979; CN110294531		REVOKED	(CN113683197)\|REVOKED	DEAD	(CN113683197)\|DEAD	(CN113683197)\|LEGAL DETAILS FOR CN113683197\|Actual or expected expiration date=2023-06-23\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2021-08-16\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202110935649\|Application date=2021-08-16\|Standardized application number=2021CN-0935649\|Event publication date=2021-11-23\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN113683197\|Publication stage code=A\|Publication date=2021-11-23\|Standardized publication number=CN113683197\|Event publication date=2021-11-23\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2021-12-10\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2023-06-23\|Event code=CN/RJ01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Rejection of an application after its publication			https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoQk2O2zXRvU8Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000059980367&ekey=2211&xpn=CN113683197&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=fcS77sZ%252Bq2lEYTuaxuvPxpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN113683197)\|CN	(CN113683197)\|NAME=ANHUI XINYU ECOLOGICAL IND CO LTD , COUNTRY=CN		(CN113683197)\|NAME=WANG XIAOJUN;Hefei Daozhi Intellectual Property Agency Co., Ltd. , REG=34130		(CN113683197)\|NAME=ZHANG YOUDE\|NAME=HE JIANJUN\|NAME=DAI CAOPEI\|NAME=ZHANG TIANTIAN	(CN113683197)\|5	1	1					(CN113683197)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2021-11-23\|Gazette number: GAZNUM=37-4801\|Number of Pages: NPAGES=9\|		(CN113683197)\|CHINESE (CHI)	(CN113683197)\|Patent	Titre: (CN113683197)\|Efficient nitrogen and phosphorus removal anti-blocking constructed wetland system Résumé: (CN113683197)\|The invention discloses an efficient nitrogen and phosphorus removal anti-blocking constructed wetland system, and relates to the technical field of constructed wetland construction. The system comprises an aeration reoxygenation chamber, an enhanced carbon removal chamber, an enhanced nitrogen removal chamber, an enhanced phosphorus removal chamber, a sludge sedimentation tank and the like. A water inlet channel is mainly used for uniformly distributing water and collecting purified water. The aeration reoxygenation chamber is a main body unit for water quality purification and mainly comprises an aeration device, composite filler and plants, and when a polluted water body flows through the unit module, the water quality can be purified by virtue of the composite filler, soil filtration, and activities of aquatic plants, high-efficiency microorganisms and the like. According to the water quality of inlet water and the water quality target needing to be achieved, different concentrated and matched fillers can be selected, so that the enhanced carbon removal chamber, the enhanced nitrogen removal chamber, the enhanced phosphorus removal chamber and the sludge sedimentation tank which are designed and obtained can effectively remove nitrogen, phosphorus, heavy metal, impurity sludge and the like in the water body.	26	Abstract	gpt-4o-mini	no	The article focuses on a constructed wetland system for nitrogen and phosphorus removal, with no mention of enhanced weathering or CO₂ capture.
26	CN202311235173	CN202311235173	CN117404069	108167543	CN117404069 A 2024-01-16 [CN117404069]	2023-09-22	2023-09-22	2024-01-16		(CN117404069)\|2043-09-22	(CN117404069)\|Coiled tubing dragging type supercritical water injection coal rock underground gasification method	(CN117404069)\|The invention provides a coiled tubing dragging type supercritical water injection coal rock underground gasification method. The method comprises the following steps that 1, water with the temperature being 374.3 DEG C or above is injected into a coal seam through a draggable continuous oil pipe, the pressure in the continuous oil pipe and the pressure of the shaft bottom are controlled to be 22.1 MPa or above, high-temperature and high-speed supercritical water jet is sprayed out to crush coal rock, the supercritical water reacts with coal to obtain combustible gas, and meanwhile a gasification cavity is formed; 2, after the gasification cavity is formed, dragging the draggable coiled tubing to a next position, and repeating the jet flow process to form another gasification cavity; and 3, discharging the combustible gas out of the ground, and carrying out gas-water separation to recover H2. According to the technical scheme, the coal underground gasification technology can assist in efficient utilization of deep coal seam resources, can be organically coupled with a carbon dioxide capture, utilization and burying technology, and is expected to effectively absorb and digest CO2 generated in the coal combustion process.	CHINA UNIVERSITY OF PETROLEUM BEIJING	(CN117404069)\|CHINA UNIVERSITY OF PETROLEUM (BEIJING) ([CN])	YANG RUIYUE\|HUANG ZHONGWEI\|JING MEIYANG\|WU XIAOGUANG\|LI JINGBIN\|HONG CHUNYANG\|CHEN JIANXIANG\|QIN XIAOZHOU	(CN117404069)\|YANG RUIYUE\|HUANG ZHONGWEI\|JING MEIYANG\|WU XIAOGUANG\|LI JINGBIN\|HONG CHUNYANG\|CHEN JIANXIANG\|QIN XIAOZHOU	(CN117404069)\|YAO LIANG;BEIJING SANYOU INTELLECTUAL PROPERTY AGENCY LTD\|Reg. Nb: 11127\|HAN LEI;BEIJING SANYOU INTELLECTUAL PROPERTY AGENCY LTD\|Reg. Nb: 11127	(CN117404069)\|The cavitation gasification method has the advantages of increasing the contact area, improving the efficiency and the like.\|	(CN117404069)\|1. A continuous oil pipe dragging type supercritical water injection coal rock underground gasification method comprises the following steps:step 1: injecting water with the temperature of 374.3 ℃ or higher into a coal bed through a draggable continuous oil pipe, controlling the pressure in the continuous oil pipe and the pressure at the bottom of the well to be 22.1MPa or higher, injecting high-temperature and high-speed supercritical water jet to break up coal and rock, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;step 2: after forming the gasification cavity, dragging the draggable continuous oil pipe to the next position, and repeating the jet flow process to form another gasification cavity;step 3: discharging the combustible gas to the ground and recovering H by gas-water separation 2 。\|	(CN117404069)\|In order to solve the technical problems, the invention aims to provide the underground coal and rock gasification method which is based on the dragging type continuous oil pipe and supercritical water injection coal and rock technology and is beneficial to the efficient utilization of deep coal seam resources. In order to achieve the above purpose, the invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|The invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method.\|The invention relates to a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, and belongs to the technical field of coal gasification.\|	(CN117404069)\|UNDERGROUND GASIFICATION CAVITY(100,1)\|COAL COMBUSTIONCO(89,1)\|DRAG GABLE OIL PIPE(86,4)\|COMBUSTIBLE GAS(84,14)\|DEEP COAL SEAM RESOURCE(72,2)\|GASIFICATION CHAMBER(65,5)\|COAL BED(62,5)\|TARGET COAL SEAM(40,2)\|BYPRODUCT(38,1)\|UNDERGROUND COAL GASIFICATION(37,2)\|FIRING(36,1)\|COILED TUBING(34,7)\|ENTIRE COAL SEAM(31,1)\|SPRAY GUN TOOL(30,4)\|COAL UNDERGROUND GASIFICATION ENGINEERING(27,1)\|FORMATION CONDITION(27,1)\|ANNULUS(26,5)\|GASIFICATION CAVITY TRANSFORMATION(17,1)\|GAS WATER SEPARATION(16,7)\|CARBON DIOXIDE(16,2)\|POWER ASSISTED(15,2)\|SUPERCRITICAL WATER INJECTION COAL(14,3)\|DEEP COAL RESERVOIR(14,1)\|MULTIPOINT TRANSFORMATION(14,1)\|ORGANIC MATTER(14,1)\|SYNCHRONOUS REFORMING(14,1)\|HORIZONTAL WELL(12,6)\|CHINA UNIVERSITY(12,1)\|COAL COMBUSTION(12,1)\|COAL ROCK(12,1)\|COMBUSTION CONTINUITY(12,1)\|COMBUSTION EXPLOITATION(12,1)\|GASIFICATION FURNACE(12,1)\|HOMOGENEOUS OXIDIZATION(12,1)\|HYDRAULIC JETTING(12,1)\|UCG ENGINEERING(12,1)\|UNDERGROUND ACCURATE BUTT JOINT(12,1)\|HEAT PRESERVATION(10,2)\|PERMEABILITY(10,2)\|WATER VAPOR(10,2)\|COMBUSTION DYNAMIC(10,1)\|DYNAMIC COMBUSTION MONITORING(10,1)\|PHOSPHATING TREATMENT(10,1)\|REFORMED CAVITY(10,1)\|SHALLOW COAL SEAM(10,1)\|SMOOTH PROCEEDING(10,1)\|CN114607278B(9,2)\|BURYING(8,1)\|COMPRESSIBILITY(8,1)\|CONTROLLABLE GAS INJECTION(8,1)\|CRIP(8,1)\|GASIFIER CONSTRUCTION(8,1)\|GEOLOGICAL CONDITION(8,1)\|GROUND SEPARATION TANK(8,1)\|PRACTICABILITY(8,1)\|RESISTANT SPRAY GUN(8,1)\|STRATUM CONDITION(8,1)\|	(CN117404069)\|1. A continuous oil pipe dragging type supercritical water injection coal rock underground gasification method comprises the following steps:\|step 1: injecting water with the temperature of 374.3 ℃ or higher into a coal bed through a draggable continuous oil pipe, controlling the pressure in the continuous oil pipe and the pressure at the bottom of the well to be 22.1MPa or higher, injecting high-temperature and high-speed supercritical water jet to break up coal and rock, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|step 2: after forming the gasification cavity, dragging the draggable continuous oil pipe to the next position, and repeating the jet flow process to form another gasification cavity;\|step 3: discharging the combustible gas to the ground and recovering H by gas-water separation 2 。\|2. The method of claim 1, wherein the step of ejecting a high temperature, high velocity supercritical water jet to break up coal rock is accomplished by a lance tool;\|preferably, the lance tool is a cavitation lance in CN114607278B or CN 111395964B.\|3. The method of claim 1, wherein the reaction of supercritical water with coal comprises:\|coal + supercritical water → CO 2 +H 2 +CH 4 ;\|CO 2 +coal→co;\|organic matter +O 2 →CO 2 +H 2 O。\|4. A method according to claim 1 or 3, wherein the method further comprises capturing and/or separating CO at the surface 2 And injecting the coal bed into the gasification cavity.\|5. The method according to claim 1 or 4, wherein CO is captured and/or separated in the gasification chamber 2 Reacts with carbon in the coal bed at high temperature to generate CO, and the CO further reacts with water vapor to generate H 2 And CO 2 And obtaining the combustible gas.\|6. The method according to claim 1 or 4, wherein the main component of the combustible gas is CH 4 、H 2 、CO。\|7. The method according to claim 1 or 4, wherein the method comprises the steps of: CO obtained by separating gas from water 2 And injecting the mixture into a gasification cavity of the coal bed to participate in the reaction in the gasification cavity.\|8. The method of claim 1, wherein the method further comprises the steps of: and drilling the horizontal well into the coal seam, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m.\|9. The method of claim 1, wherein step 2 is repeated and the number of times the gasification chamber is formed is adjusted according to the actual formation conditions until the entire coal seam is fully utilized.\|10. The method according to any one of claims 1-9, comprising the specific steps of:\|(1) Drilling a horizontal well to a target coal seam, wherein the distances between the horizontal well and a top plate and a bottom plate of the coal seam are respectively more than or equal to 1m;\|(2) A continuous oil pipe provided with a spray gun tool is put into a coal bed;\|(3) Injecting high-temperature water with the temperature of more than 374.3 ℃ into the coiled tubing from the ground;\|(4) Controlling the pressure in the coiled tubing and the pressure at the bottom of the well to be more than 22.1MPa, spraying high-temperature and high-speed supercritical water jet at the bottom of the well to break coal and rock at the bottom of the well, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|(5) After forming the gasification cavity, dragging the continuous oil pipe to the next position, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|(6) The combustible gas is discharged out of the ground through an annulus, and H is recovered after gas-water separation on the ground 2 ;\|(7) Separating the ground from the obtained CO 2 The byproducts are re-injected into the underground gasification cavity to participate in the reaction in the gasification cavity.	(CN117404069)\|TECHNICAL FIELD\|[0001] The invention relates to a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, and belongs to the technical field of coal gasification.\|BACKGROUND ART\|[0002] Underground coal gasification technology (UCG) is controlled combustion of underground coal in situ to produce CH 4 、H 2 The process of combustible gas such as CO and the like is a coal clean development and utilization technology integrating three processes of well construction, coal mining and gasification, can promote the development and utilization of deep coal seams, greatly improves the resource utilization efficiency, is used as a potential coal clean exploitation means, is not applied in a large scale due to the restriction of factors such as technology and economy, and still is in an engineering test stage and needs to be subjected to key technology attack. In addition, the existing engineering test projects mainly adopt shallow coal seams, and the technology is relatively mature.\|[0003] However, compared with the shallow coal seam, the underground gasification of the deep coal is more advantageous in the aspect of environmental protection, but the deep coal seam has the characteristics of high ground stress, medium and high temperature, extremely low permeability, high saturation, strong compressibility and the like, and the key technology for restricting the development of the underground gasification of the deep coal is further required to be overcome.\|[0004] In recent years, the key engineering technology of the UCG (deep coal reservoir) mainly surrounds the U-shaped gasifier construction technology and the controllable gas injection point back-off gasification process (CRIP). However, because underground coal gasification is in-situ combustion exploitation of coal, in order to keep combustion continuity, the drilling rate of a coal bed in a horizontal well section is theoretically required to reach 100%, and the well track control of the horizontal well and the underground accurate butt joint of the horizontal well and a production vertical well bring great challenges to the construction of a U-shaped gasification furnace. The CRIP technology is applicable to the feasibility of deep coal underground gasification engineering, but the coal seam is shallower in the current field test, and the applicability is still to be further practically checked.\|DISCLOSURE\|Disclosure of Invention\|[0005] In order to solve the technical problems, the invention aims to provide the underground coal and rock gasification method which is based on the dragging type continuous oil pipe and supercritical water injection coal and rock technology and is beneficial to the efficient utilization of deep coal seam resources.\|[0006] In order to achieve the above purpose, the invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|[0007] step 1: injecting water with the temperature of 374.3 ℃ or higher into a coal bed through a draggable continuous oil pipe, controlling the pressure in the continuous oil pipe and the pressure at the bottom of the well to be 22.1MPa or higher, injecting high-temperature and high-speed supercritical water jet to break up coal and rock, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|[0008] step 2: after forming the gasification cavity, dragging the draggable continuous oil pipe to the next position, and repeating the jet flow process to form another gasification cavity;\|[0009] step 3: discharging the combustible gas to the ground and recovering H by gas-water separation 2 。\|[0010] According to a specific embodiment of the present invention, preferably, the high temperature water is heated at the surface to a temperature of not less than 374.3 ℃ and then injected into the coal seam through the coiled tubing.\|[0011] According to the specific embodiment of the invention, preferably, the high-temperature water is injected by adopting an oil pipe, and the annular space is in a closed state in the process, so that the heat preservation effect is realized while the bottom hole pressure is controlled.\|[0012] According to the specific embodiment of the invention, the pressure in the oil pipe and the bottom hole pressure are preferably controlled to be more than 22.1MPa, so that the injected high temperature water can be in a supercritical state at 374.3 ℃.\|[0013] According to a specific embodiment of the present invention, preferably, the step of ejecting the supercritical water jet at high temperature and high speed to break up coal and rock is implemented by a spray gun tool.\|[0014] According to a specific embodiment of the present invention, preferably, the spray gun tool is a hole-making spray gun in CN114607278B or CN111395964B, which has good temperature and pressure resistance.\|[0015] According to the specific embodiment of the invention, the high-temperature high-speed supercritical water jet flow is adopted to efficiently break the coal and rock, so that the subsequent reaction is quickened, the gasification cavity transformation effect is improved, the construction time is shortened, and the construction cost is saved. Meanwhile, jet flow can generate stress disturbance to form a pressure relief area, so that pressure relief, reflection increase and income improvement are realized, and cost reduction and efficiency increase are achieved.\|[0016] According to the specific embodiment of the invention, the supercritical water forms supercritical water jet flow through the spray gun tool, so that the supercritical water continuously reacts with coal to convert coal chemical energy into hydrogen energy due to the characteristics of high temperature and high pressure, homogeneous oxidation and the like of the supercritical water while efficiently breaking coal and rock. Preferably, the reaction of supercritical water with coal comprises:\|[0017] coal + supercritical water → CO 2 +H 2 +CH 4 ;\|[0018] CO 2 +coal→co;\|[0019] organic matter +O 2 →CO 2 +H 2 O。\|[0020] According to a particular embodiment of the invention, the CO is preferably to be captured and/or separated at the surface 2 And injecting the coal bed into the gasification cavity.\|[0021] According to a particular embodiment of the invention, the CO is preferably captured and/or separated in the gasification chamber 2 Reacts with carbon in the coal seam at high temperature to produce CO, which further reacts with water vapor (formed from supercritical water) to produce H 2 And CO 2 And obtaining the combustible gas.\|[0022] According to a specific embodiment of the present invention, preferably, the main component of the combustible gas is CH 4 、H 2 CO, etc.\|[0023] According to a specific embodiment of the present invention, preferably, the combustible gas formed in the gasification chamber is exhausted to the ground through the annulus, and the produced fluid is subjected to gas-water separation in the ground separation tank, and clean fuel H is separated and recovered 2 。\|[0024] According to a specific embodiment of the invention, preferably, the method comprises the steps of: will beCO obtained by gas-water separation 2 And injecting the mixture into a gasification cavity of the coal bed to participate in the reaction in the gasification cavity. Through the reciprocating circulation process, the method is expected to effectively absorb and digest CO generated in the coal combustion process 2 。\|[0025] According to a specific embodiment of the present invention, preferably, the method further comprises the steps of: and drilling the horizontal well into the coal seam, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m.\|[0026] According to a specific embodiment of the present invention, the step 2 is preferably repeated, and the number of times of forming the gasification chamber is repeated is adjusted according to the actual stratum condition until the whole coal seam is fully utilized.\|[0027] According to a particular embodiment of the invention, the method preferably comprises the following specific steps:\|[0028] (1) Drilling a horizontal well to a target coal seam, wherein the distances between the horizontal well and a top plate and a bottom plate of the coal seam are respectively more than or equal to 1m;\|[0029] (2) A continuous oil pipe provided with a spray gun tool is put into a coal bed;\|[0030] (3) Injecting high-temperature water with the temperature of more than 374.3 ℃ into the coiled tubing from the ground;\|[0031] (4) Controlling the pressure in the coiled tubing and the pressure at the bottom of the well to be more than 22.1MPa, spraying high-temperature and high-speed supercritical water jet at the bottom of the well to break coal and rock at the bottom of the well, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|[0032] (5) After smoothly reforming the gasification cavity, dragging the continuous oil pipe to the next position, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|[0033] (6) The combustible gas is discharged out of the ground through an annulus, and H is recovered after gas-water separation on the ground 2 ;\|[0034] (7) Separating the ground from the obtained CO 2 The byproducts are re-injected into the underground gasification cavity to participate in the reaction in the gasification cavity.\|[0035] The continuous oil pipe dragging type supercritical water injection coal rock underground gasification method provided by the invention is suitable for deep coal seam resources, such as deep coal seams with the burial depth of 1500-3000 m.\|[0036] The technical scheme of the invention is that the Underground Coal Gasification (UCG) technology can be used for capturing and utilizing carbon dioxide and is organically coupled with the burying technology (UCG-CCUS) while the power-assisted deep coal seam resources are utilized efficiently, and is expected to effectively absorb and digest CO generated in the coal combustion process 2 。\|[0037] The method provided by the invention breaks the coal and rock by means of supercritical water jet impact, and breaks the coal and rock to improve the construction efficiency and gasification efficiency while forming a better reaction cavity, and can react in the gasification cavity, so that the gasification can be easier to carry out by breaking the coal blocks, the effect is better, and the jet can generate stress disturbance to form a pressure relief area, so that the pressure relief and permeability improvement can be realized. The cavitation gasification method has the advantages of increasing the contact area, improving the efficiency and the like. In addition, the method provided by the invention can realize multi-point transformation through one well and one pipe column, does not need ignition of a combustion well, has simple process, strong practicability and low cost, and can be used for transformation of a deep coal seam.\|[0038] The invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method by combining the advantages of a CRIP process, a continuous oil pipe technology and a supercritical water jet technology. The method of the invention can not only convey gasifying agent and igniter to the bottom of the well in UCG engineering, but also bind with temperature, pressure and other sensors to realize the combustion dynamic monitoring function, thereby controlling the injection of gasifying agent according to geological conditions and coal bed characteristics to ensure that the whole combustion process is stable and the produced components are optimal.\|DRAWINGS DESCRIPTION\|[0039] Fig. 1 is a schematic diagram of a coal underground gasification method of coiled tubing dragging type supercritical water injection coal rock according to embodiment 1 of the present invention.\|INVENTION MODE\|Detailed Description\|[0040] The technical solution of the present invention will be described in detail below for a clearer understanding of technical features, objects and advantageous effects of the present invention, but should not be construed as limiting the scope of the present invention.\|[0041] Example 1\|[0042] The embodiment provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|[0043] (1) Drilling a horizontal well to a gasification reforming target coal seam with a burial depth of 1500-3000m, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m, so that the whole process is smoothly carried out in the target coal seam;\|[0044] (2) The continuous oil pipe is utilized to send a spray gun tool to a preset reconstruction point, the spray gun tool uses a high-pressure resistant, temperature resistant and wear resistant spray gun (a hole-making spray gun in CN114607278B, CN 111395964B) developed by China university of Petroleum (Beijing), the bearing temperature is-30 ℃ to 100 ℃, the working pressure bearing pressure is 70MPa at maximum, the surface is subjected to phosphating treatment, the corrosion resistance is enhanced, the spraying speed can reach 250m/s, and the coal rock can be efficiently impacted and broken;\|[0045] (3) Injecting high-temperature water with the temperature of more than or equal to 374.3 ℃ into the coiled tubing from the ground, injecting the high-temperature water into the tubing, wherein an annulus is in a closed state in the process, controlling the bottom hole pressure and simultaneously playing a role in heat preservation;\|[0046] (4) The pressure in the continuous oil pipe and the pressure at the bottom of the well are controlled at 22.1MPa, high-temperature and high-speed supercritical water jet is sprayed at the bottom of the well, the characteristics of high temperature and high pressure, homogeneous oxidization and the like of supercritical water are utilized to continuously react with coal while the coal is crushed, a large amount of heat is released in the reaction process, the smooth proceeding of the subsequent reaction is maintained, the coal chemical energy is converted into hydrogen energy in the whole process, the combustible gas is obtained, and a gasification cavity is formed;\|[0047] (5) After the gasification cavity is formed, the synchronous reforming effect of pressure relief and permeability increase can be achieved on the coal bed around the reformed cavity during reaction, and the gas yield is increased. After a first gasification cavity is smoothly transformed, dragging the continuous oil pipe to the next position, transforming the point spacing to 20m, determining a plurality of transformation points by adopting a geometric dividing method, dragging a spray gun by using the continuous oil pipe, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|[0048] (6) Discharging the combustible gas (gas-water mixture) from the ground through the annulus, and recovering H after gas-water separation on the ground 2 ;\|[0049] (7) Separating the ground from the obtained CO 2 Gasification chamber with byproduct reinjection into the groundThe gasification chamber is used for trapping and utilizing again.\|[0050] Fig. 1 is a schematic diagram of a coal underground gasification method of coiled tubing dragging type supercritical water injection coal rock according to embodiment 1 of the present invention. The dragging type continuous oil pipe can realize fixed-point, directional and multiple hydraulic jetting, can be combined with monitoring technologies such as temperature, pressure and the like to realize dynamic combustion monitoring, and reasonably selects the cavity-building times according to site construction conditions, construction requirements, reservoir conditions and the like.	(CN117404069)\|TECHNICAL FIELD\|[0001] The invention relates to a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, and belongs to the technical field of coal gasification.\|BACKGROUND ART\|[0002] Underground coal gasification technology (UCG) is controlled combustion of underground coal in situ to produce CH 4 、H 2 The process of combustible gas such as CO and the like is a coal clean development and utilization technology integrating three processes of well construction, coal mining and gasification, can promote the development and utilization of deep coal seams, greatly improves the resource utilization efficiency, is used as a potential coal clean exploitation means, is not applied in a large scale due to the restriction of factors such as technology and economy, and still is in an engineering test stage and needs to be subjected to key technology attack. In addition, the existing engineering test projects mainly adopt shallow coal seams, and the technology is relatively mature.\|[0003] However, compared with the shallow coal seam, the underground gasification of the deep coal is more advantageous in the aspect of environmental protection, but the deep coal seam has the characteristics of high ground stress, medium and high temperature, extremely low permeability, high saturation, strong compressibility and the like, and the key technology for restricting the development of the underground gasification of the deep coal is further required to be overcome.\|[0004] In recent years, the key engineering technology of the UCG (deep coal reservoir) mainly surrounds the U-shaped gasifier construction technology and the controllable gas injection point back-off gasification process (CRIP). However, because underground coal gasification is in-situ combustion exploitation of coal, in order to keep combustion continuity, the drilling rate of a coal bed in a horizontal well section is theoretically required to reach 100%, and the well track control of the horizontal well and the underground accurate butt joint of the horizontal well and a production vertical well bring great challenges to the construction of a U-shaped gasification furnace. The CRIP technology is applicable to the feasibility of deep coal underground gasification engineering, but the coal seam is shallower in the current field test, and the applicability is still to be further practically checked.\|DISCLOSURE\|Disclosure of Invention\|[0005] In order to solve the technical problems, the invention aims to provide the underground coal and rock gasification method which is based on the dragging type continuous oil pipe and supercritical water injection coal and rock technology and is beneficial to the efficient utilization of deep coal seam resources.\|[0006] In order to achieve the above purpose, the invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|[0007] step 1: injecting water with the temperature of 374.3 ℃ or higher into a coal bed through a draggable continuous oil pipe, controlling the pressure in the continuous oil pipe and the pressure at the bottom of the well to be 22.1MPa or higher, injecting high-temperature and high-speed supercritical water jet to break up coal and rock, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|[0008] step 2: after forming the gasification cavity, dragging the draggable continuous oil pipe to the next position, and repeating the jet flow process to form another gasification cavity;\|[0009] step 3: discharging the combustible gas to the ground and recovering H by gas-water separation 2 。\|[0010] According to a specific embodiment of the present invention, preferably, the high temperature water is heated at the surface to a temperature of not less than 374.3 ℃ and then injected into the coal seam through the coiled tubing.\|[0011] According to the specific embodiment of the invention, preferably, the high-temperature water is injected by adopting an oil pipe, and the annular space is in a closed state in the process, so that the heat preservation effect is realized while the bottom hole pressure is controlled.\|[0012] According to the specific embodiment of the invention, the pressure in the oil pipe and the bottom hole pressure are preferably controlled to be more than 22.1MPa, so that the injected high temperature water can be in a supercritical state at 374.3 ℃.\|[0013] According to a specific embodiment of the present invention, preferably, the step of ejecting the supercritical water jet at high temperature and high speed to break up coal and rock is implemented by a spray gun tool.\|[0014] According to a specific embodiment of the present invention, preferably, the spray gun tool is a hole-making spray gun in CN114607278B or CN111395964B, which has good temperature and pressure resistance.\|[0015] According to the specific embodiment of the invention, the high-temperature high-speed supercritical water jet flow is adopted to efficiently break the coal and rock, so that the subsequent reaction is quickened, the gasification cavity transformation effect is improved, the construction time is shortened, and the construction cost is saved. Meanwhile, jet flow can generate stress disturbance to form a pressure relief area, so that pressure relief, reflection increase and income improvement are realized, and cost reduction and efficiency increase are achieved.\|[0016] According to the specific embodiment of the invention, the supercritical water forms supercritical water jet flow through the spray gun tool, so that the supercritical water continuously reacts with coal to convert coal chemical energy into hydrogen energy due to the characteristics of high temperature and high pressure, homogeneous oxidation and the like of the supercritical water while efficiently breaking coal and rock. Preferably, the reaction of supercritical water with coal comprises:\|[0017] coal + supercritical water → CO 2 +H 2 +CH 4 ;\|[0018] CO 2 +coal→co;\|[0019] organic matter +O 2 →CO 2 +H 2 O。\|[0020] According to a particular embodiment of the invention, the CO is preferably to be captured and/or separated at the surface 2 And injecting the coal bed into the gasification cavity.\|[0021] According to a particular embodiment of the invention, the CO is preferably captured and/or separated in the gasification chamber 2 Reacts with carbon in the coal seam at high temperature to produce CO, which further reacts with water vapor (formed from supercritical water) to produce H 2 And CO 2 And obtaining the combustible gas.\|[0022] According to a specific embodiment of the present invention, preferably, the main component of the combustible gas is CH 4 、H 2 CO, etc.\|[0023] According to a specific embodiment of the present invention, preferably, the combustible gas formed in the gasification chamber is exhausted to the ground through the annulus, and the produced fluid is subjected to gas-water separation in the ground separation tank, and clean fuel H is separated and recovered 2 。\|[0024] According to a specific embodiment of the invention, preferably, the method comprises the steps of: will beCO obtained by gas-water separation 2 And injecting the mixture into a gasification cavity of the coal bed to participate in the reaction in the gasification cavity. Through the reciprocating circulation process, the method is expected to effectively absorb and digest CO generated in the coal combustion process 2 。\|[0025] According to a specific embodiment of the present invention, preferably, the method further comprises the steps of: and drilling the horizontal well into the coal seam, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m.\|[0026] According to a specific embodiment of the present invention, the step 2 is preferably repeated, and the number of times of forming the gasification chamber is repeated is adjusted according to the actual stratum condition until the whole coal seam is fully utilized.\|[0027] According to a particular embodiment of the invention, the method preferably comprises the following specific steps:\|[0028] (1) Drilling a horizontal well to a target coal seam, wherein the distances between the horizontal well and a top plate and a bottom plate of the coal seam are respectively more than or equal to 1m;\|[0029] (2) A continuous oil pipe provided with a spray gun tool is put into a coal bed;\|[0030] (3) Injecting high-temperature water with the temperature of more than 374.3 ℃ into the coiled tubing from the ground;\|[0031] (4) Controlling the pressure in the coiled tubing and the pressure at the bottom of the well to be more than 22.1MPa, spraying high-temperature and high-speed supercritical water jet at the bottom of the well to break coal and rock at the bottom of the well, enabling supercritical water to react with coal to obtain combustible gas, and forming a gasification cavity;\|[0032] (5) After smoothly reforming the gasification cavity, dragging the continuous oil pipe to the next position, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|[0033] (6) The combustible gas is discharged out of the ground through an annulus, and H is recovered after gas-water separation on the ground 2 ;\|[0034] (7) Separating the ground from the obtained CO 2 The byproducts are re-injected into the underground gasification cavity to participate in the reaction in the gasification cavity.\|[0035] The continuous oil pipe dragging type supercritical water injection coal rock underground gasification method provided by the invention is suitable for deep coal seam resources, such as deep coal seams with the burial depth of 1500-3000 m.\|[0036] The technical scheme of the invention is that the Underground Coal Gasification (UCG) technology can be used for capturing and utilizing carbon dioxide and is organically coupled with the burying technology (UCG-CCUS) while the power-assisted deep coal seam resources are utilized efficiently, and is expected to effectively absorb and digest CO generated in the coal combustion process 2 。\|[0037] The method provided by the invention breaks the coal and rock by means of supercritical water jet impact, and breaks the coal and rock to improve the construction efficiency and gasification efficiency while forming a better reaction cavity, and can react in the gasification cavity, so that the gasification can be easier to carry out by breaking the coal blocks, the effect is better, and the jet can generate stress disturbance to form a pressure relief area, so that the pressure relief and permeability improvement can be realized. The cavitation gasification method has the advantages of increasing the contact area, improving the efficiency and the like. In addition, the method provided by the invention can realize multi-point transformation through one well and one pipe column, does not need ignition of a combustion well, has simple process, strong practicability and low cost, and can be used for transformation of a deep coal seam.\|[0038] The invention provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method by combining the advantages of a CRIP process, a continuous oil pipe technology and a supercritical water jet technology. The method of the invention can not only convey gasifying agent and igniter to the bottom of the well in UCG engineering, but also bind with temperature, pressure and other sensors to realize the combustion dynamic monitoring function, thereby controlling the injection of gasifying agent according to geological conditions and coal bed characteristics to ensure that the whole combustion process is stable and the produced components are optimal.\|DRAWINGS DESCRIPTION\|[0039] Fig. 1 is a schematic diagram of a coal underground gasification method of coiled tubing dragging type supercritical water injection coal rock according to embodiment 1 of the present invention.\|INVENTION MODE\|Detailed Description\|[0040] The technical solution of the present invention will be described in detail below for a clearer understanding of technical features, objects and advantageous effects of the present invention, but should not be construed as limiting the scope of the present invention.\|[0041] Example 1\|[0042] The embodiment provides a continuous oil pipe dragging type supercritical water injection coal rock underground gasification method, which comprises the following steps:\|[0043] (1) Drilling a horizontal well to a gasification reforming target coal seam with a burial depth of 1500-3000m, wherein the distances between the horizontal well and the top plate and the bottom plate of the coal seam are respectively more than or equal to 1m, so that the whole process is smoothly carried out in the target coal seam;\|[0044] (2) The continuous oil pipe is utilized to send a spray gun tool to a preset reconstruction point, the spray gun tool uses a high-pressure resistant, temperature resistant and wear resistant spray gun (a hole-making spray gun in CN114607278B, CN 111395964B) developed by China university of Petroleum (Beijing), the bearing temperature is-30 ℃ to 100 ℃, the working pressure bearing pressure is 70MPa at maximum, the surface is subjected to phosphating treatment, the corrosion resistance is enhanced, the spraying speed can reach 250m/s, and the coal rock can be efficiently impacted and broken;\|[0045] (3) Injecting high-temperature water with the temperature of more than or equal to 374.3 ℃ into the coiled tubing from the ground, injecting the high-temperature water into the tubing, wherein an annulus is in a closed state in the process, controlling the bottom hole pressure and simultaneously playing a role in heat preservation;\|[0046] (4) The pressure in the continuous oil pipe and the pressure at the bottom of the well are controlled at 22.1MPa, high-temperature and high-speed supercritical water jet is sprayed at the bottom of the well, the characteristics of high temperature and high pressure, homogeneous oxidization and the like of supercritical water are utilized to continuously react with coal while the coal is crushed, a large amount of heat is released in the reaction process, the smooth proceeding of the subsequent reaction is maintained, the coal chemical energy is converted into hydrogen energy in the whole process, the combustible gas is obtained, and a gasification cavity is formed;\|[0047] (5) After the gasification cavity is formed, the synchronous reforming effect of pressure relief and permeability increase can be achieved on the coal bed around the reformed cavity during reaction, and the gas yield is increased. After a first gasification cavity is smoothly transformed, dragging the continuous oil pipe to the next position, transforming the point spacing to 20m, determining a plurality of transformation points by adopting a geometric dividing method, dragging a spray gun by using the continuous oil pipe, and repeating the steps (3) and (4), thereby forming a plurality of gasification cavities;\|[0048] (6) Discharging the combustible gas (gas-water mixture) from the ground through the annulus, and recovering H after gas-water separation on the ground 2 ;\|[0049] (7) Separating the ground from the obtained CO 2 Gasification chamber with byproduct reinjection into the groundThe gasification chamber is used for trapping and utilizing again.\|[0050] Fig. 1 is a schematic diagram of a coal underground gasification method of coiled tubing dragging type supercritical water injection coal rock according to embodiment 1 of the present invention. The dragging type continuous oil pipe can realize fixed-point, directional and multiple hydraulic jetting, can be combined with monitoring technologies such as temperature, pressure and the like to realize dynamic combustion monitoring, and reasonably selects the cavity-building times according to site construction conditions, construction requirements, reservoir conditions and the like.	Family Number\|(108167543)\|108167543\|Abstract\|(CN117404069 A)\|The invention provides a coiled tubing dragging type supercritical water injection coal rock underground gasification method . The method comprises the following steps that 1, water with the temperature being 374.3 DEG C or above is injected into a coal seam through a draggable continuous oil pipe , the pressure in the continuous oil pipe and the pressure of the shaft bottom are controlled to be 22.1 MPa or above , high - temperature and high - speed supercritical water jet is sprayed out to crush coal rock , the supercritical water reacts with coal to obtain combustible gas , and meanwhile a gasification cavity is formed ; 2, after the gasification cavity is formed , dragging the draggable coiled tubing to a next position , and repeating the jet flow process to form another gasification cavity ; and 3, discharging the combustible gas out of the ground , and carrying out gas - water separation to recover H2 . According to the technical scheme , the coal underground gasification technology can assist in efficient utilization of deep coal seam resources , can be organically coupled with a carbon dioxide capture , utilization and burying technology , and is expected to effectively absorb and digest CO2 generated in the coal combustion process . \|	Civil engineering	E21B-043/295\|E21B-047/00		E21B-043/295\|E21B-047/00	E21B-043/295\|E21B-047/00	E21B-043/295\|E21B-047/00			CN117823112B	CN117823112B 109209909 WHO=Examiner SELF=N	CN116575900\|CN114607278\|CN114607278B\|CN111395964\|CN110552678\|CN115853488\|CN101113670\|US20100288555	CN116575900 106093745 WHO=Examiner SELF=N CAT=Y\|CN114607278 100436537 WHO=Examiner SELF=Y CAT=Y\|CN114607278B 100436537 WHO=Examiner SELF=Y CAT=Y\|CN111395964 89650997 WHO=Examiner SELF=Y CAT=Y\|CN110552678 86927074 WHO=Examiner SELF=N CAT=Y\|CN115853488 104311160 WHO=Examiner SELF=N CAT=A\|CN101113670 6492399 WHO=Examiner SELF=N CAT=A\|US20100288555 14121274 WHO=Examiner SELF=N CAT=A		CN101113670; US20100288555; CN110552678; CN111395964; CN114607278; CN115853488; CN114607278B; CN116575900		PENDING	(CN117404069)\|PENDING	ALIVE	(CN117404069)\|ALIVE	(CN117404069)\|LEGAL DETAILS FOR CN117404069\|Actual or expected expiration date=2043-09-22\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-09-22\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202311235173\|Application date=2023-09-22\|Standardized application number=2023CN-1235173\|Event publication date=2024-01-16\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN117404069\|Publication stage code=A\|Publication date=2024-01-16\|Standardized publication number=CN117404069\|Event publication date=2024-01-16\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2024-02-02\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN117404069)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoRcmltkk1GC9Vfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000071091443&ekey=1977&xpn=CN117404069&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=maHWLlLw9yeEcraFRbWWSZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN117404069)\|CN	(CN117404069)\|NAME=CHINA UNIVERSITY OF PETROLEUM (BEIJING) , COUNTRY=CN		(CN117404069)\|NAME=YAO LIANG;BEIJING SANYOU INTELLECTUAL PROPERTY AGENCY LTD , REG=11127NAME=HAN LEI;BEIJING SANYOU INTELLECTUAL PROPERTY AGENCY LTD , REG=11127		(CN117404069)\|NAME=YANG RUIYUE\|NAME=HUANG ZHONGWEI\|NAME=JING MEIYANG\|NAME=WU XIAOGUANG\|NAME=LI JINGBIN\|NAME=HONG CHUNYANG\|NAME=CHEN JIANXIANG\|NAME=QIN XIAOZHOU	(CN117404069)\|1	1	1					(CN117404069)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2024-01-16\|Gazette number: GAZNUM=40-0301\|Number of Pages: NPAGES=7\|		(CN117404069)\|CHINESE (CHI)	(CN117404069)\|Patent	Titre: (CN117404069)\|Coiled tubing dragging type supercritical water injection coal rock underground gasification method Résumé: (CN117404069)\|The invention provides a coiled tubing dragging type supercritical water injection coal rock underground gasification method. The method comprises the following steps that 1, water with the temperature being 374.3 DEG C or above is injected into a coal seam through a draggable continuous oil pipe, the pressure in the continuous oil pipe and the pressure of the shaft bottom are controlled to be 22.1 MPa or above, high-temperature and high-speed supercritical water jet is sprayed out to crush coal rock, the supercritical water reacts with coal to obtain combustible gas, and meanwhile a gasification cavity is formed; 2, after the gasification cavity is formed, dragging the draggable coiled tubing to a next position, and repeating the jet flow process to form another gasification cavity; and 3, discharging the combustible gas out of the ground, and carrying out gas-water separation to recover H2. According to the technical scheme, the coal underground gasification technology can assist in efficient utilization of deep coal seam resources, can be organically coupled with a carbon dioxide capture, utilization and burying technology, and is expected to effectively absorb and digest CO2 generated in the coal combustion process.	25	Abstract	gpt-4o-mini	no	The article focuses on underground gasification of coal and CO2 capture related to combustion, not on accelerated weathering or mineral carbonation processes.
27	CN202410256237	CN202410256237	CN117918078	109552031	CN117918078 A 2024-04-26 [CN117918078]	2024-03-06	2024-03-06	2024-04-26		(CN117918078)\|2044-03-06	(CN117918078)\|Method for improving soil and increasing carbon sink	(CN117918078)\|The invention discloses a method capable of improving soil and increasing carbon sink, and relates to the technical field of soil improvement, the method comprises a crusher and a dolomite raw material, the mined dolomite raw material is put into the crusher to obtain a small-size blocky dolomite raw material, the small-size blocky dolomite raw material is put into a preset grinding machine, and the grinding machine is used for grinding the small-size blocky dolomite raw material; the method comprises the following steps: crushing ground calcium carbonate to obtain powdery ground calcium carbonate, further containing the powdery ground calcium carbonate in an automatic scattering barrel, carrying the automatic scattering barrel through a preset unmanned aerial vehicle, and further uniformly scattering the powdery ground calcium carbonate into an external pretreatment ecological system; calcium carbonate in the ground calcium carbonate is attached to land and is subjected to a weathering reaction with rock, carbon dioxide in air is captured, an associated reaction is generated, and divalent calcium and bicarbonate radicals are obtained through the reaction. The soil conditioner can reduce acidity of soil, is beneficial to soil remediation, increases nutrient elements of the soil, and enhances the soil improvement effect.	INSTITUTE OF GEOCHEMISTRY - CHINESE ACADEMY OF SCIENCES	(CN117918078)\|INSTITUTE OF GEOCHEMISTRY CHINESE ACADEMY OF SCIENCES ([CN])	SHI LIANGXING\|CENG SIBO\|LIU ZAIHUA	(CN117918078)\|SHI LIANGXING\|CENG SIBO\|LIU ZAIHUA	(CN117918078)\|ZHANG XIAODONG;Beijing Blue Spider Patent Agency Co., Ltd.\|Reg. Nb: 16226	(CN117918078)\|1. the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application.\|The method has the advantages that the acidity of soil can be reduced by increasing the photosynthesis of the aquatic organisms absorbed by clean CO 2, the soil is beneficial to the restoration of the soil, the nutrient elements of the soil are increased, and the soil improvement effect is enhanced.\|The working principle is as follows: the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application.\|The above reasons lead to the fact that the existing soil is high in acidity, the soil is difficult to repair, the soil is poor in quality and lacks of nutrient substances, and the utilization rate of the soil is low.\|	(CN117918078)\|1. The method for improving soil and increasing carbon sink comprises a crusher and dolomite raw materials, and is characterized in that the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic scattering bucket, the automatic scattering bucket is carried by a preset unmanned plane, and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment; The calcium carbonate in the heavy calcium carbonate is attached to land, and is subjected to weathering reaction with rock to capture carbon dioxide in the air, and an accompanying reaction is generated to obtain divalent calcium and bicarbonate, so that calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment.\|	(CN117918078)\|The invention discloses a method capable of realizing soil improvement and increasing carbon sequestration, which relates to the technical field of soil improvement and comprises a crusher and dolomite raw materials, wherein the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic sprinkling barrel, the automatic sprinkling barrel is carried by a preset unmanned aerial vehicle, and the powdery heavy calcium carbonate is further uniformly sprinkled into an external pretreatment ecological system; the calcium carbonate in the heavy calcium carbonate is attached to land, and undergoes weathering reaction with rock to capture carbon dioxide in the air, and accompanying reaction is generated, so that divalent calcium and bicarbonate are obtained through the reaction.\|The invention relates to the technical field of soil improvement, in particular to a method capable of achieving soil improvement and increasing carbon sink.\|	(CN117918078)\|GROUND(100,16)\|CARBON SINK(100,13)\|SOIL IMPROVEMENT(100,9)\|AUTOMATIC SPRINKLING BARREL(99,2)\|POWDERY HEAVY CALCIUM CARBONATE(91,11)\|HEAVY POWDER(86,12)\|SOIL RESTORATION(64,2)\|PRESET GRINDER(58,4)\|CALCIUM CARBONATE(54,38)\|DIVALENT CALCIUM(49,4)\|PRESET UNMANNED PLANE(48,1)\|CRUSHER(47,7)\|CALCIUM CARBONATE CAPTURE(41,2)\|NUTRIENT SUBSTANCE(38,1)\|HEAVY CALCIUM CARBONATE(36,10)\|BICARBONATE(34,7)\|PRETREATMENT(34,5)\|MAGNESIUM ION(32,9)\|DIC FERTILIZATION(32,6)\|SMALL VOLUME BLOCKY DOLOMITE(31,8)\|SOIL AGGLOMERATE(31,1)\|RELIEVING ACIDIFICATION(28,5)\|PRESET UNMANNED AERIAL VEHICLE(28,3)\|CARBON SEQUESTRATION(27,3)\|RESTORATION TREATMENT(27,3)\|MINED DOLOMITE RAW MATERIAL(26,4)\|DOLOMITE RAW MATERIAL(25,7)\|BUCKET(22,6)\|PHOTOSYNTHESIS(22,2)\|WATER ALKALIZATION(21,1)\|ACIDITY(20,1)\|SMALL VOLUME BLOCKY(19,8)\|ROCK(19,3)\|CARBON DIOXIDE(17,16)\|BICARBONATE ION(17,3)\|DISSOLUTION REACTION(17,3)\|CARBONATE ION REACTION(17,2)\|PRETREATMENT ECOLOGICAL SYSTEM(17,2)\|EFFECTING SOIL IMPROVEMENT(17,1)\|AQUATIC ECOSYSTEM(16,6)\|LAND ECOLOGICAL SYSTEM(16,3)\|UNMANNED AERIAL VEHICLE(16,3)\|AQUATIC ORGANISM(15,5)\|RAW MATERIAL(14,15)\|ECOLOGICAL SYSTEM(14,10)\|REACTION PRODUCT(13,3)\|SOIL FERTILITY(12,4)\|CALCIUM ION(11,8)\|GREENHOUSE EFFECT(11,3)\|SOIL AGGREGATE(10,3)\|CACO(10,2)\|LARGE AREA POPULARIZATION(9,2)\|LOW COST BENEFIT(9,2)\|UTILIZATION RATE(9,1)\|LIGHT ACTION(8,1)\|CHEMICAL EQUATION(7,6)\|CO2(7,3)\|SOIL SUSTAINABILITY(7,1)\|DISSOLVED INORGANIC CARBON(6,12)\|ENDOGENOUS ORGANIC CARBON AOC(6,3)\|H2O MG(6,2)\|ABSORB NUTRIENT(6,1)\|SOIL ENVIRONMENT ECOLOGY(6,1)\|ABSORB AQUATIC ORGANISM(5,1)\|ABSORPTION AQUATIC ORGANISM(4,1)\|MOISTURE MANAGEMENT(4,1)\|WATER BODY ALKALIZATION(3,4)\|	(CN117918078)\|1. The method for improving soil and increasing carbon sink comprises a crusher and dolomite raw materials, and is characterized in that the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic scattering bucket, the automatic scattering bucket is carried by a preset unmanned plane, and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment;\| The calcium carbonate in the heavy calcium carbonate is attached to land, and is subjected to weathering reaction with rock to capture carbon dioxide in the air, and an accompanying reaction is generated to obtain divalent calcium and bicarbonate, so that calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. \|2. The method of claim 1, wherein the accompanying reaction comprises chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, and reacting the carbonate ions with carbon dioxide and water in the presence of sufficient carbon dioxide to produce bicarbonate ions.\|3. The method for improving soil and increasing carbon sequestration according to claim 2, wherein the chemical equation of the chemical dissolution reaction of heavy calcium carbonate with water is: mgCO 3+CaCO3+H2O—Mg2++Ca2++2CO32-.\|4. The method for improving soil and increasing carbon dioxide according to claim 2, wherein the chemical equation of the reaction of carbonate ions and carbon dioxide is CO 32-+CO2+H2O—2HCO3-.\|5. A method of effecting soil improvement and carbon sequestration according to claim 3 wherein said calcium and magnesium ions enter the soil system to form soil agglomerates which alter soil fertility.\|6. The method of claim 1, wherein the calcium carbonate is weathered to produce dissolved inorganic carbon, the dissolved inorganic carbon enters the aquatic ecosystem, the water is absorbed by adding clean CO 2, and light action occurs, so that the DIC fertilization effect is utilized to form an endogenous organic carbon AOC, and further, the organic carbon capable of relieving acidification or alkalization of the water is formed and stored in the water.	(CN117918078)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of soil improvement, in particular to a method capable of achieving soil improvement and increasing carbon sink.\|BACKGROUND ART\|[0002] Soil improvement refers to improving the texture, structure, fertility and moisture retention of soil through a series of measures and methods to increase the agricultural productivity and sustainability of the soil. The soil improvement method comprises the following steps: organic matter addition, mineral addition, pH adjustment, and moisture management.\|[0003] Carbon sink refers to a natural or artificial system capable of absorbing and storing isothermal chamber gases of carbon dioxide (CO 2). They can help reduce the greenhouse gas content in the atmosphere and mitigate global climate change. Natural carbon sinks include forest, wetland, grassland, ocean and other ecosystems. An artificial carbon sink is an artificially created system for absorbing and storing carbon dioxide.\|[0004] In the process of production activities, on one hand, human beings easily interfere with the soil surface layer and vegetation in the peripheral area of the production activities, so that the soil structure function is destroyed, the carbon sink capacity of the soil is reduced, and effective soil aggregates can not be formed to prevent loss of nutrients, thereby reducing the soil fertility and causing land degradation; on the other hand, in the soil which is partially engaged in production activities, such as mines, the large content of heavy metals can damage the capability of plants to absorb other nutrient elements, influence the microbial activity in the soil, and reduce the number of plants and microorganisms.\|[0005] The above reasons lead to the fact that the existing soil is high in acidity, the soil is difficult to repair, the soil is poor in quality and lacks of nutrient substances, and the utilization rate of the soil is low.\|[0006] The above information disclosed in this background section is only for enhancement of understanding of the background section of the invention and therefore it may not form the prior art that is already known to those of ordinary skill in the art.\|DISCLOSURE\|Disclosure of Invention\|[0007] Aiming at the technical problems existing in the existing soil ecological environment, the invention provides a method for improving soil and increasing carbon sink.\|[0008] The method for improving soil and increasing carbon sink comprises the steps of putting the mined dolomite raw materials into a crusher to obtain small-volume blocky dolomite raw materials, putting the small-volume blocky dolomite raw materials into a preset grinder to obtain powdery heavy calcium carbonate, further placing the powdery heavy calcium carbonate into an automatic scattering bucket, and carrying the automatic scattering bucket through a preset unmanned aerial vehicle to uniformly scatter the powdery heavy calcium carbonate into an external pretreatment ecological system;\|[0009] The calcium carbonate in the heavy calcium carbonate is attached to land, and is subjected to weathering reaction with rock to capture carbon dioxide in the air, and an accompanying reaction is generated to obtain divalent calcium and bicarbonate, so that calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. \|[0010] Further, the accompanying reaction comprises chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, and the carbonate ions react with carbon dioxide and water to generate bicarbonate ions in an environment with enough carbon dioxide.\|[0011] Further, the chemical equation of the chemical dissolution reaction of the heavy calcium carbonate and water is as follows: caMgCO 3+H2O+CO2—Mg2++Ca2++2HCO32-.\|[0012] Further, the chemical equation of the reaction of the carbonate ions and the carbon dioxide is CO 32-+CO2+H2O—2HCO3-.\|[0013] Further, the calcium ions and magnesium ions enter the soil system to form soil aggregates which can change the soil fertility.\|[0014] Furthermore, the calcium carbonate is weathered to generate dissolved inorganic carbon, the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed by adding clean CO 2, a light effect is generated, and further an endogenous organic carbon AOC is formed by using a DIC fertilization effect, so that organic carbon capable of relieving acidification or alkalization of a water body is formed and stored in the water body.\|[0015] The foregoing summary is for the purpose of the specification only and is not intended to be limiting in any way. In addition to the illustrative aspects, embodiments, and features described above, further aspects, embodiments, and features of the present invention will become apparent by reference to the drawings and the following detailed description.\|[0016] The invention has the beneficial effects that:\|[0017] 1. the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application. \|[0018] 2. The dissolved inorganic carbon is generated through calcium carbonate weathering, so that the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed through adding clean CO 2, the light effect is generated, and further, an endogenous organic carbon AOC is formed by using a DIC fertilization effect, and further, the organic carbon capable of relieving acidification or alkalization of a water body is formed to be stored in the water body, so that acidification of the water body can be relieved conveniently.\|DRAWINGS DESCRIPTION\|[0019] FIG. 1 is a schematic illustration of the reaction scheme of the present invention;\|[0020] Fig. 2 is a schematic diagram of the workflow of the present invention. \|INVENTION MODE\|Detailed Description\|[0021] It is noted that the figures are schematic and not drawn to scale. Relative dimensions and proportions of parts of the figures have been shown exaggerated or reduced in size, for the sake of clarity and convenience in the drawings, and any dimensions are merely illustrative and not limiting. The same reference numerals are used for the same structures, elements, or accessories appearing in more than two figures to embody similar features.\|[0022] Examples\|[0023] A method for improving soil and increasing carbon sink comprises a crusher and dolomite raw materials, wherein the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic scattering bucket, the automatic scattering bucket is carried by a preset unmanned aerial vehicle, and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment, such as a mine and an acidified water body.\|[0024] The calcium carbonate in heavy calcium carbonate is attached to land, and undergoes weathering reaction with rock to capture carbon dioxide in air, and accompanying reaction is generated, so that divalent calcium and bicarbonate are obtained through the reaction, and then calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. The calcium carbonate is ground into powder and is scattered into a land ecological system, so that the calcium carbonate can capture atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere can be reduced conveniently, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved.\|[0025] The accompanying reaction comprises the chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, wherein the chemical equation of the chemical dissolution reaction of the heavy calcium carbonate and water is as follows: mgCO 3+CaCO3+H2O—Mg2++Ca2++2CO32-. Calcium ions and magnesium ions enter the soil system to form soil aggregates which can change the soil fertility. The method has the advantages that the acidity of soil can be reduced by increasing the photosynthesis of the aquatic organisms absorbed by clean CO 2, the soil is beneficial to the restoration of the soil, the nutrient elements of the soil are increased, and the soil improvement effect is enhanced.\|[0026] And in the presence of sufficient carbon dioxide, the carbonate ions react with carbon dioxide and water to form bicarbonate ions. The chemical equation for the reaction of carbonate ions with carbon dioxide is CO 32-+CO2+H2O—2HCO3-. The calcium carbonate is weathered to generate dissolved inorganic carbon, the dissolved inorganic carbon enters into an aquatic ecosystem, the clean CO 2 is added to absorb aquatic organisms, the light effect is generated, and then the DIC fertilization effect is utilized to form endogenous organic carbon AOC, so that organic carbon capable of relieving acidification or alkalization of the water body is formed and stored in the water body. The dissolved inorganic carbon is generated through calcium carbonate weathering, so that the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed through adding clean CO 2, the light effect is generated, and further, an endogenous organic carbon AOC is formed by using a DIC fertilization effect, and further, the organic carbon capable of relieving acidification or alkalization of a water body is formed to be stored in the water body, so that acidification of the water body can be relieved conveniently.\|[0027] The working principle is as follows: the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application.\|[0028] And then through the calcium carbonate efflorescence production dissolved inorganic carbon, make dissolved inorganic carbon enter into aquatic ecosystem, through increasing clean CO 2 absorption aquatic organism, take place the photosynthesis, and then utilize DIC fertilization effect to form endogenous organic carbon AOC, and then form can alleviate the organic carbon of water acidizing or alkalization and preserve to the water in, be convenient for can alleviate the acidizing of water.\|[0029] In the description of the present invention, the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. The meaning of "a plurality of" is two or more, unless specifically defined otherwise.\|[0030] In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0031] In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.\|[0032] In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily for the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.\|[0033] In the drawings of the disclosed embodiments, only the structures related to the embodiments of the present disclosure are referred to, and other structures may refer to the general design, so that the same embodiment and different embodiments of the present disclosure may be combined with each other without conflict.\|[0034] Although the present invention has been described with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described, or equivalents may be substituted for elements thereof, and any modifications, equivalents, improvements and changes may be made without departing from the spirit and principles of the present invention.	(CN117918078)\|TECHNICAL FIELD\|Technical Field\|[0001] The invention relates to the technical field of soil improvement, in particular to a method capable of achieving soil improvement and increasing carbon sink.\|BACKGROUND ART\|[0002] Soil improvement refers to improving the texture, structure, fertility and moisture retention of soil through a series of measures and methods to increase the agricultural productivity and sustainability of the soil. The soil improvement method comprises the following steps: organic matter addition, mineral addition, pH adjustment, and moisture management.\|[0003] Carbon sink refers to a natural or artificial system capable of absorbing and storing isothermal chamber gases of carbon dioxide (CO 2). They can help reduce the greenhouse gas content in the atmosphere and mitigate global climate change. Natural carbon sinks include forest, wetland, grassland, ocean and other ecosystems. An artificial carbon sink is an artificially created system for absorbing and storing carbon dioxide.\|[0004] In the process of production activities, on one hand, human beings easily interfere with the soil surface layer and vegetation in the peripheral area of the production activities, so that the soil structure function is destroyed, the carbon sink capacity of the soil is reduced, and effective soil aggregates can not be formed to prevent loss of nutrients, thereby reducing the soil fertility and causing land degradation; on the other hand, in the soil which is partially engaged in production activities, such as mines, the large content of heavy metals can damage the capability of plants to absorb other nutrient elements, influence the microbial activity in the soil, and reduce the number of plants and microorganisms.\|[0005] The above reasons lead to the fact that the existing soil is high in acidity, the soil is difficult to repair, the soil is poor in quality and lacks of nutrient substances, and the utilization rate of the soil is low.\|[0006] The above information disclosed in this background section is only for enhancement of understanding of the background section of the invention and therefore it may not form the prior art that is already known to those of ordinary skill in the art.\|DISCLOSURE\|Disclosure of Invention\|[0007] Aiming at the technical problems existing in the existing soil ecological environment, the invention provides a method for improving soil and increasing carbon sink.\|[0008] The method for improving soil and increasing carbon sink comprises the steps of putting the mined dolomite raw materials into a crusher to obtain small-volume blocky dolomite raw materials, putting the small-volume blocky dolomite raw materials into a preset grinder to obtain powdery heavy calcium carbonate, further placing the powdery heavy calcium carbonate into an automatic scattering bucket, and carrying the automatic scattering bucket through a preset unmanned aerial vehicle to uniformly scatter the powdery heavy calcium carbonate into an external pretreatment ecological system;\|[0009] The calcium carbonate in the heavy calcium carbonate is attached to land, and is subjected to weathering reaction with rock to capture carbon dioxide in the air, and an accompanying reaction is generated to obtain divalent calcium and bicarbonate, so that calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. \|[0010] Further, the accompanying reaction comprises chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, and the carbonate ions react with carbon dioxide and water to generate bicarbonate ions in an environment with enough carbon dioxide.\|[0011] Further, the chemical equation of the chemical dissolution reaction of the heavy calcium carbonate and water is as follows: caMgCO 3+H2O+CO2—Mg2++Ca2++2HCO32-.\|[0012] Further, the chemical equation of the reaction of the carbonate ions and the carbon dioxide is CO 32-+CO2+H2O—2HCO3-.\|[0013] Further, the calcium ions and magnesium ions enter the soil system to form soil aggregates which can change the soil fertility.\|[0014] Furthermore, the calcium carbonate is weathered to generate dissolved inorganic carbon, the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed by adding clean CO 2, a light effect is generated, and further an endogenous organic carbon AOC is formed by using a DIC fertilization effect, so that organic carbon capable of relieving acidification or alkalization of a water body is formed and stored in the water body.\|[0015] The foregoing summary is for the purpose of the specification only and is not intended to be limiting in any way. In addition to the illustrative aspects, embodiments, and features described above, further aspects, embodiments, and features of the present invention will become apparent by reference to the drawings and the following detailed description.\|[0016] The invention has the beneficial effects that:\|[0017] 1. the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application. \|[0018] 2. The dissolved inorganic carbon is generated through calcium carbonate weathering, so that the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed through adding clean CO 2, the light effect is generated, and further, an endogenous organic carbon AOC is formed by using a DIC fertilization effect, and further, the organic carbon capable of relieving acidification or alkalization of a water body is formed to be stored in the water body, so that acidification of the water body can be relieved conveniently.\|DRAWINGS DESCRIPTION\|[0019] FIG. 1 is a schematic illustration of the reaction scheme of the present invention;\|[0020] Fig. 2 is a schematic diagram of the workflow of the present invention. \|INVENTION MODE\|Detailed Description\|[0021] It is noted that the figures are schematic and not drawn to scale. Relative dimensions and proportions of parts of the figures have been shown exaggerated or reduced in size, for the sake of clarity and convenience in the drawings, and any dimensions are merely illustrative and not limiting. The same reference numerals are used for the same structures, elements, or accessories appearing in more than two figures to embody similar features.\|[0022] Examples\|[0023] A method for improving soil and increasing carbon sink comprises a crusher and dolomite raw materials, wherein the mined dolomite raw materials are placed into the crusher to obtain small-volume blocky dolomite raw materials, the small-volume blocky dolomite raw materials are placed into a preset grinder to obtain powdery heavy calcium carbonate, the powdery heavy calcium carbonate is further contained in an automatic scattering bucket, the automatic scattering bucket is carried by a preset unmanned aerial vehicle, and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment, such as a mine and an acidified water body.\|[0024] The calcium carbonate in heavy calcium carbonate is attached to land, and undergoes weathering reaction with rock to capture carbon dioxide in air, and accompanying reaction is generated, so that divalent calcium and bicarbonate are obtained through the reaction, and then calcium ions, magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment for restoration treatment. The calcium carbonate is ground into powder and is scattered into a land ecological system, so that the calcium carbonate can capture atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere can be reduced conveniently, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved.\|[0025] The accompanying reaction comprises the chemical dissolution of water and heavy calcium carbonate to obtain magnesium ions, calcium ions and carbonate ions, wherein the chemical equation of the chemical dissolution reaction of the heavy calcium carbonate and water is as follows: mgCO 3+CaCO3+H2O—Mg2++Ca2++2CO32-. Calcium ions and magnesium ions enter the soil system to form soil aggregates which can change the soil fertility. The method has the advantages that the acidity of soil can be reduced by increasing the photosynthesis of the aquatic organisms absorbed by clean CO 2, the soil is beneficial to the restoration of the soil, the nutrient elements of the soil are increased, and the soil improvement effect is enhanced.\|[0026] And in the presence of sufficient carbon dioxide, the carbonate ions react with carbon dioxide and water to form bicarbonate ions. The chemical equation for the reaction of carbonate ions with carbon dioxide is CO 32-+CO2+H2O—2HCO3-. The calcium carbonate is weathered to generate dissolved inorganic carbon, the dissolved inorganic carbon enters into an aquatic ecosystem, the clean CO 2 is added to absorb aquatic organisms, the light effect is generated, and then the DIC fertilization effect is utilized to form endogenous organic carbon AOC, so that organic carbon capable of relieving acidification or alkalization of the water body is formed and stored in the water body. The dissolved inorganic carbon is generated through calcium carbonate weathering, so that the dissolved inorganic carbon enters into an aquatic ecosystem, aquatic organisms are absorbed through adding clean CO 2, the light effect is generated, and further, an endogenous organic carbon AOC is formed by using a DIC fertilization effect, and further, the organic carbon capable of relieving acidification or alkalization of a water body is formed to be stored in the water body, so that acidification of the water body can be relieved conveniently.\|[0027] The working principle is as follows: the calcium carbonate is ground into powder and scattered into a land ecological system, so that the calcium carbonate captures the atmospheric CO 2 through rock weathering, the content of CO 2 in the atmosphere is reduced, a certain effect of increasing carbon sink is achieved, and the greenhouse effect caused by CO 2 is further relieved; the method has the advantages of simple operation, simple flow, low cost and considerable benefit, and is suitable for large-area popularization and application.\|[0028] And then through the calcium carbonate efflorescence production dissolved inorganic carbon, make dissolved inorganic carbon enter into aquatic ecosystem, through increasing clean CO 2 absorption aquatic organism, take place the photosynthesis, and then utilize DIC fertilization effect to form endogenous organic carbon AOC, and then form can alleviate the organic carbon of water acidizing or alkalization and preserve to the water in, be convenient for can alleviate the acidizing of water.\|[0029] In the description of the present invention, the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. The meaning of "a plurality of" is two or more, unless specifically defined otherwise.\|[0030] In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.\|[0031] In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.\|[0032] In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily for the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.\|[0033] In the drawings of the disclosed embodiments, only the structures related to the embodiments of the present disclosure are referred to, and other structures may refer to the general design, so that the same embodiment and different embodiments of the present disclosure may be combined with each other without conflict.\|[0034] Although the present invention has been described with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described, or equivalents may be substituted for elements thereof, and any modifications, equivalents, improvements and changes may be made without departing from the spirit and principles of the present invention.	Family Number\|(109552031)\|109552031\|Object of Invention\|(CN117918078 A)\|The invention discloses a method capable of realizing soil improvement and increasing carbon sequestration , which relates to the technical field of soil improvement and comprises a crusher and dolomite raw materials , wherein the ( . . . ) pretreatment ecological system ; the calcium carbonate in the heavy calcium carbonate is attached to land , and undergoes weathering reaction with rock to capture carbon dioxide in the air , and accompanying reaction is generated , so that divalent calcium and bicarbonate are obtained through the reaction . \|Abstract\|(CN117918078 A)\|The invention discloses a method capable of improving soil and increasing carbon sink , and relates to the technical field of soil improvement , the method comprises a crusher and a dolomite raw material , the mined dolomite raw material is put into the crusher to obtain a small - size blocky dolomite raw material , the small - size blocky dolomite raw material is put into a preset grinding machine , and the grinding machine is used for grinding the small - size blocky dolomite raw material ; the method comprises the following steps : crushing ground calcium carbonate to obtain powdery ground calcium carbonate , further containing the powdery ground calcium carbonate in an automatic scattering barrel , carrying the automatic scattering barrel through a preset unmanned aerial vehicle , and further uniformly scattering the powdery ground calcium carbonate into an external pretreatment ecological system ; calcium carbonate in the ground calcium carbonate is attached to land and is subjected to a weathering reaction with rock , carbon dioxide in air is captured , an associated reaction is generated , and divalent calcium and bicarbonate radicals are obtained through the reaction . The soil conditioner can reduce acidity of soil , is beneficial to soil remediation , increases nutrient elements of the soil , and enhances the soil improvement effect . \|Advantages / Prev. Drawbacks\|(CN117918078 A)\|1. the calcium carbonate is ground into powder and scattered into a land ecological system , so that the calcium carbonate captures the atmospheric CO 2 through rock weathering , the content of CO 2 in the atmosphere is reduced , a certain effect of increasing carbon sink is achieved , and the greenhouse effect caused by CO 2 is further relieved ; the method has the advantages of simple operation , simple flow , low cost ( . . . ) \|The working principle is as follows : the calcium carbonate is ground into powder and scattered into a land ecological system , so that the calcium carbonate captures the atmospheric CO 2 through rock weathering , the content of CO 2 in the atmosphere is reduced , a certain effect of increasing carbon sink is achieved , and the greenhouse effect caused by CO 2 is further relieved ; the method has the advantages of simple operation , simple flow , low cost ( . . . ) \|Independent Claims\|(CN117918078 A)\|( . . . ) unmanned plane , and the powdery heavy calcium carbonate is further uniformly scattered into an ecological system subjected to external pretreatment ; The calcium carbonate in the heavy calcium carbonate is attached to land , and is subjected to weathering reaction with rock to capture carbon dioxide in the air , and an accompanying reaction is generated to obtain divalent calcium and bicarbonate , so that calcium ions , magnesium ions and bicarbonate which are reaction products enter an ecological system subjected to external pretreatment ( . . . ) \|	Other special machines	A01B-077/00\|A01B-079/00		A01B-077/00\|A01B-079/00	A01B-077/00\|A01B-079/00	A01B-077/00\|A01B-079/00					CN117101374\|CN106190157\|CN105295930	CN117101374 107464098 WHO=Examiner SELF=N CAT=A\|CN106190157 74809241 WHO=Examiner SELF=N CAT=A\|CN105295930 72139248 WHO=Examiner SELF=N CAT=A	李长江等: "《园林绿化与养护》", 31 January 2024, 中国电力出版社, pages: 213 - 214 (Cat. Y)\|安艳玲: "《贵州清水江流域生态环境保护与可持续管理》", 31 July 2017, 中国环境出版社, pages: 38 - 39 (Cat. Y)	CN105295930; CN106190157; CN117101374		PENDING	(CN117918078)\|PENDING	ALIVE	(CN117918078)\|ALIVE	(CN117918078)\|LEGAL DETAILS FOR CN117918078\|Actual or expected expiration date=2044-03-06\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-06\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202410256237\|Application date=2024-03-06\|Standardized application number=2024CN-0256237\|Event publication date=2024-04-26\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN117918078\|Publication stage code=A\|Publication date=2024-04-26\|Standardized publication number=CN117918078\|Event publication date=2024-04-26\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2024-05-14\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN117918078)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTaLIaZYZJUQFfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000072418778&ekey=2208&xpn=CN117918078&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=Dc8j7iM%252FQW1wtnlTbS5ktpNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN117918078)\|CN	(CN117918078)\|NAME=INSTITUTE OF GEOCHEMISTRY CHINESE ACADEMY OF SCIENCES , COUNTRY=CN		(CN117918078)\|NAME=ZHANG XIAODONG;Beijing Blue Spider Patent Agency Co., Ltd. , REG=16226		(CN117918078)\|NAME=SHI LIANGXING\|NAME=CENG SIBO\|NAME=LIU ZAIHUA	(CN117918078)\|2	1	1					(CN117918078)\|Number of Claims: NCL=6\|Gazette date: GAZDATE=2024-04-26\|Gazette number: GAZNUM=40-1702\|Number of Pages: NPAGES=8\|		(CN117918078)\|CHINESE (CHI)	(CN117918078)\|Patent	Titre: (CN117918078)\|Method for improving soil and increasing carbon sink Résumé: (CN117918078)\|The invention discloses a method capable of improving soil and increasing carbon sink, and relates to the technical field of soil improvement, the method comprises a crusher and a dolomite raw material, the mined dolomite raw material is put into the crusher to obtain a small-size blocky dolomite raw material, the small-size blocky dolomite raw material is put into a preset grinding machine, and the grinding machine is used for grinding the small-size blocky dolomite raw material; the method comprises the following steps: crushing ground calcium carbonate to obtain powdery ground calcium carbonate, further containing the powdery ground calcium carbonate in an automatic scattering barrel, carrying the automatic scattering barrel through a preset unmanned aerial vehicle, and further uniformly scattering the powdery ground calcium carbonate into an external pretreatment ecological system; calcium carbonate in the ground calcium carbonate is attached to land and is subjected to a weathering reaction with rock, carbon dioxide in air is captured, an associated reaction is generated, and divalent calcium and bicarbonate radicals are obtained through the reaction. The soil conditioner can reduce acidity of soil, is beneficial to soil remediation, increases nutrient elements of the soil, and enhances the soil improvement effect.	24	Abstract	gpt-4o-mini	yes	The method involves the use of dolomite and calcium carbonate to enhance soil, capture CO₂ through weathering reactions, and produce bicarbonates, aligning with the goals of accelerated weathering and carbon sequestration.
28	US61/152,220\|US61/152,220P\|US12/701,156\|WOUS2010/023740	VE2010-000234\|WOUS2010/023740\|IN1897/MUMNP/2011\|MA34162\|ZA201106558\|EG2011081359\|TN2011000396\|BRPI1008447\|EP10741655\|MX2011008525\|UAA201110768\|AU2010213862\|EA201171023\|CN201080016478\|AP2011005878\|IL214555\|CA2752524\|GEAP2010012380\|MYPI2011003742\|PE2011001483\|US12/701,156	BRPI1008447\|GEP20146167\|EP2406353\|MY152266\|MX319678\|UA104616\|EG26451\|AU2010213862\|TN2011000396\|ZA201106558\|US8323481\|VE2010000234\|PE20120704\|EA201171023\|CN102395657\|MA33117\|IN1897/MUMNP/2011\|EP2406353\|MX2011008525\|AP2011005878\|IL214555\|AU2010213862\|WO2010/093684\|CA2752524\|WO2010/093684\|US20100200465	35298	VE2010000234 A 2012-07-26 [VE2010000234]\|WO2010/093684 A3 2010-11-18 [WO201093684]\|WO2010/093684 A2 2010-08-19 [WO201093684]\|IN1897/MUMNP/2011 A 2012-02-03 [IN2011MN01897]\|MA33117 B1 2012-03-01 [MA--33117]\|ZA201106558 B 2013-02-27 [ZA201106558]\|EG26451 A 2013-11-12 [EG--26451]\|TN2011000396 A1 2013-03-27 [TN2011000396]\|BRPI1008447 A2 2019-09-24 [BR201008447]\|EP2406353 A4 2014-09-17 [EP2406353]\|EP2406353 A2 2012-01-18 [EP2406353]\|MX319678 B 2014-04-24 [MX-319678]\|MX2011008525 A 2011-12-16 [MX2011008525]\|UA104616 C2 2014-02-25 [UA-104616]\|AU2010213862 B2 2013-05-02 [AU2010213862]\|AU2010213862 A1 2011-09-22 [AU2010213862]\|EA201171023 A1 2012-03-30 [EA201171023]\|CN102395657 A 2012-03-28 [CN102395657]\|AP2011005878 A0 2011-10-31 [AP2011005878]\|IL214555 A 2011-09-27 [IL-214555]\|CA2752524 A1 2010-08-19 [CA2752524]\|GEP20146167 B 2014-09-25 [GE201406167]\|MY152266 A 2014-09-15 [MY-152266]\|PE20120704 A1 2012-06-27 [PE201200704]\|US8323481 B2 2012-12-04 [US8323481]\|US20100200465 A1 2010-08-12 [US20100200465]	2009-02-12\|2010-02-05\|2010-02-10	2010-02-12\|2010-02-10\|2011-09-10\|2011-09-09\|2011-09-07\|2011-08-11\|2011-08-09\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-10\|2010-02-05	2019-09-24\|2014-09-25\|2014-09-17\|2014-09-15\|2014-04-24\|2014-02-25\|2013-11-12\|2013-05-02\|2013-03-27\|2013-02-27\|2012-12-04\|2012-07-26\|2012-06-27\|2012-03-30\|2012-03-28\|2012-03-01\|2012-02-03\|2012-01-18\|2011-12-16\|2011-10-31\|2011-09-27\|2011-09-22\|2010-11-18\|2010-08-19\|2010-08-19\|2010-08-12	\|(US8323481)\|2012-12-04\|\|\|(GE201406167)\|2014-09-25\|(MY-152266)\|2014-09-15\|(MX-319678)\|2014-04-24\|(UA-104616)\|2014-02-25\|(EG--26451)\|2013-11-12\|(AU2010213862)\|2013-05-02\|(ZA201106558)\|2013-02-27\|(MA--33117)\|2012-03-01\|\|\|\|\|\|\|\|\|	(EP2406353)\|2015-03-20\|(US8323481)\|2025-01-06\|(WO2010/093684)\|2012-08-12\|(CN102395657)\|2015-01-14\|(GEP20146167)\|2030-02-10\|(MY152266)\|2030-02-10\|(MX319678)\|2030-02-10\|(UA104616)\|2030-02-10\|(EG26451)\|2030-02-10\|(AU2010213862)\|2015-09-03\|(ZA201106558)\|2030-02-10\|(MA33117)\|2030-02-10\|(BRPI1008447)\|2019-10-01\|(TN2011000396)\|2030-02-10\|(VE2010000234)\|2017-07-26\|(PE20120704)\|2016-05-30\|(EA201171023)\|2017-03-30\|(IN1897/MUMNP/2011)\|2022-02-03\|(AP2011005878)\|2016-10-31\|(IL214555)\|2016-09-27\|(CA2752524)\|2016-02-10	(EP2406353)\|Carbon management and sequestration from encapsulated control infrastructures	(EP2406353)\|A method of sequestering carbon dioxide emissions during recovery of hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure (100). This constructed infrastructure (100) defines a substantially encapsulated volume. A comminuted hydrocarbonaceous material can be introduced into the control infrastructure (100) to form a permeable body (120) of hydrocarbonaceous material. The permeable body (120) can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure (100) is a fixed structure. Additionally, during heating, any carbon dioxide that is produced can be sequestered. Removed hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.	RED LEAF RESOURCES	(EP2406353)\|Red Leaf Resources, Inc. ([US])\|(EP2406353)\|Red Leaf Resources, Inc. ([US])\|(US8323481)\|Red Leaf Resources, Inc. ([US])\|(US20100200465)\|DANA TODD\|PATTEN JAMES W\|(WO2010/093684)\|RED LEAF RESOURCES, INC.\|(WO2010/093684)\|RED LEAF RESOURCES, INC. ([US])\|(CN102395657)\|RED LEAF RESOURCES INC. ([US])\|(GEP20146167)\|RED LEAF RESOURCES, INC.\|(MY152266)\|RED LEAF RESOURCES, INC.\|(MX319678)\|RED LEAF RESOURCES INC* ([US])\|(MX2011008525)\|RED LEAF RESOURCES INC*\|(UA104616)\|RED LEAF RESOURCES, INC.\|(EG26451)\|RED LEAF RESOURCES INC\|(AU2010213862)\|Red Leaf Resources, Inc.\|(AU2010213862)\|Red Leaf Resources, Inc.\|(ZA201106558)\|RED LEAF RESOURCES INC\|(MA33117)\|RED LEAF RESOURCES, INC.\|(BRPI1008447)\|Red Leaf Resources, Inc\|(TN2011000396)\|RED LEAF RESOURCES, INC.\|\|(PE20120704)\|RED LEAF RESOURCES, INC.\|\|(IN1897/MUMNP/2011)\|RED LEAF RESOURCES INC ([US])\|(AP2011005878)\|RED LEAF RESOURCES INC\|(IL214555)\|RED LEAF RESOURCES, INC\|(CA2752524)\|RED LEAF RESOURCES, INC. ([US])	DANA TODD\|PATTEN JAMES W	(EP2406353)\|DANA, Todd\|PATTEN, James, W.\|(EP2406353)\|DANA, Todd\|PATTEN, James, W.	(EP2406353)\|Walker, Ross Thomson;Forresters ([DE])\|Reg. Nb: 101298687\|(US8323481)\|Thorpe North & Western LLP\|(WO2010/093684)\|ERICKSEN, Erik S. et al. ([US])\|(CN102395657)\|ZHAO RONGMIN;JEEKAI & PARTNERS\|Reg. Nb: 11245\|(MX319678)\|MARIA ANGELICA PARDAVELL JUAREZ\|(AU2010213862)\|FB Rice ([AU])\|(VE2010000234)\|LINARES ALLOCA MARLIN ENEIDA\|(CA2752524)\|BERESKIN & PARR LLP/S.E.N.C.R.L.,S.R.L. ([CA])	(US8323481)\|As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required.\|Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|In some cases it can be desirable to provide a single type of hydro carbonaceous material so that the permeable body consists essentially of one of the above materials.\|In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants.\|More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body.\|Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like.\|	(US8323481)\|1. A method of sequestering carbon dioxide emissions during recovery of hydrocarbons from hydrocarbonaceous materials comprising: a) forming a constructed permeability control infrastructure which defines a substantially encapsulated volume, said infrastructure comprising clay, bentonite clay, bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, engineered cementitious composites (ECC), fiber reinforced composites, geosynthetic fabrics, sealant, grout, compacted earth, low grade shale, or combinations thereof, wherein the control infrastructure is formed in direct contact with walls of an excavated hydrocarbonaceous material deposit or is freestanding having either a foundation support of earthen material or a local surface topography as a floor; b) introducing a comminuted hydrocarbonaceous material into the control infrastructure to form a permeable body of hydrocarbonaceous material; c) heating the permeable body sufficient to remove hydrocarbons therefrom such that the hydrocarbonaceous material is substantially stationary during heating; d) sequestering carbon dioxide produced during the heating; and e) collecting the removed hydrocarbons.\|	(US8323481)\|In another aspect, walls of the impoundment can be acid, water, and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water.\|In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|In yet another detailed aspect, the permeable body can further comprise an additive or biomass.\|	(US8323481)\|HYDROCARBONACEOUS MATERIAL(100,31)\|HYDROCARBON RECOVERY(100,6)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|BENTONITE AMENDED SOIL(71,3)\|NANOCARBON FULLERENE ADDITIVE(67,2)\|BENTONITE CLAY(53,5)\|GRADE SHALE(43,3)\|SOIL AMENDMENT(43,3)\|GEOSYNTHETIC FABRICS(43,2)\|RESISTANT PVC LINER(40,2)\|SOIL COMPACTION(38,3)\|GEOTEXTILE BAG(38,2)\|ATMOSPHERIC POLLUTANT(38,1)\|METHANEDIONE(37,41)\|SOLVENT RECOVERY(34,2)\|CLAY LINING(33,1)\|SYNTHETIC GEOGRID(32,2)\|COMPACTED FILL(31,6)\|ACID HALIDE(31,1)\|RESIN ION EXCHANGE(31,1)\|METHANEDIONE PRODUCTION(30,1)\|INFRASTRUCTURE(27,25)\|METHANEDIONE PRECIPITATION(27,3)\|CARBONATE DECOMPOSITION(27,2)\|OIL SHALE ORE(27,1)\|SYNTHETIC CLAY(27,1)\|ENCAPSULATED VOLUME(26,20)\|ENORMOUS VOLUME CAPACITY(26,1)\|SUPPORTING FOUNDATION(25,1)\|CONSTRUCTED PERMEABILITY(24,12)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(24,5)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|SEALANT(23,3)\|CO2 EMISSION(23,2)\|POLYMERIC RESIN(23,2)\|TEMPERATURE GEOMEMBRANE(23,1)\|CRYOGENIC PRECIPITATION(22,3)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,3)\|SOLUTION MINING(22,1)\|CONTROL INFRASTRUCTURE(21,24)\|REFRACTORY CEMENT(21,5)\|BRINE SOLUTION(21,1)\|ELECTROPLATING(21,1)\|EXTRACT FLUID(21,1)\|PERMEABILITY(20,25)\|LIQUID METHANEDIONE(20,11)\|GROUT(20,4)\|REBAR(20,4)\|FLOTATION(19,1)\|IMPOUNDMENT WALL(18,12)\|HYDRO CARBONACEOUS MATERIAL(18,6)\|LEACHING(18,1)\|GUIDELINE(17,4)\|REMOVING HYDROCARBON(16,6)\|EARTHEN MATERIAL FOUNDATION SUPPORT(16,1)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(15,10)\|FIBERGLASS(15,4)\|BRINE(15,1)\|CLAY(13,7)\|ENGINEERED CEMENTITIOUS COMPOSITE(13,4)\|BIOMASS(13,3)\|PRECIPITATION(13,3)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|AQUEOUS SOLUTION(12,7)\|ADDITIVE(11,12)\|CEMENT(11,7)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|EARTHEN MATERIAL(11,3)\|FIBER REINFORCED COMPOSITE(11,2)\|DRAIN PIPE(11,1)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|MECHANICAL INTEGRITY(11,1)\|RESISTANCE HEATER(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|INFRASTRUCTURE OPERATING TEMPERATURE(10,1)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|EXTRACTION(9,2)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,12)\|SILICATE(8,3)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|VOID VOLUME(7,7)\|FUEL CELL(7,5)\|MATERIAL DEPOSITION(7,4)\|RADIO FREQUENCY(7,4)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ECONOMIC VALUE(7,1)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|UNDISTURBED GEOLOGICAL FORMATION(6,4)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|ECONOMICALLY COMPETITIVE RECOVERY(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|SALT WATER(5,5)\|PRECIOUS METAL(5,4)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|HYDROCARBON COMBUSTION(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEATING MINED RUBBLE(5,1)\|HEATING RESIDENCE TIME(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|METHANEDIONE COLLECTION(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PERMEABILITY BALANCE(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|HEAT TRANSFER(4,10)\|LIQUID PRODUCT(4,10)\|CASE INTERIOR(4,9)\|HYDROGEN DONOR(4,7)\|HEAVY METAL(4,4)\|BLASTING(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|ECONOMICS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|SURFACE TOPOGRAPHY(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|RECLAMATION(3,2)\|STOICHIOMETRIC CONDITION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|CO2 PRODUCTION(3,1)\|COAL CONTENT(3,1)\|COMMINUTED HYDRO CARBONACEOUS MATERIAL(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|FUTURE DATE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HARVESTED HYDRO CARBONACEOUS MATERIAL(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|INTERIOR CIRCUMSTANCE(3,1)\|INTERIOR HYDROCARBONACEOUS FORMATION(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|LONG HEATING RESIDENCE TIME(3,1)\|MICROBIOLOGY(3,1)\|MINED HYDRO CARBONACEOUS MATERIAL(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|CURVATURE(2,2)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BENTONITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DIFFICULT CHALLENGE(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|FUNCTION VOID SPACE(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|INTERIOR ADDITIVE(2,1)\|INTERIOR CO2(2,1)\|INTERIOR RESIDUAL HYDROCARBON PRODUCT(2,1)\|\|(US20100200465)\|INFRASTRUCTURE(100,25)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDRO CARBONACEOUS MATERIAL(100,8)\|HYDROCARBON RECOVERY(100,6)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|METHANEDIONE COLLECTION(60,4)\|METHANEDIONE(54,49)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,22)\|ATMOSPHERIC POLLUTANT(38,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(34,6)\|SOLVENT RECOVERY(34,2)\|CRYOGENIC PRECIPITATION(33,4)\|CLAY LINING(33,1)\|ACID HALIDE(31,1)\|RESIN ION EXCHANGE(31,1)\|METHANEDIONE PRODUCTION(30,1)\|LIQUID METHANEDIONE(29,13)\|CONTROL INFRASTRUCTURE(28,28)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(28,14)\|IMPOUNDMENT(27,55)\|PERMEABILITY(27,27)\|BENTONITE CLAY(27,3)\|CARBONATE DECOMPOSITION(27,2)\|OIL SHALE ORE(27,1)\|SYNTHETIC CLAY(27,1)\|ENORMOUS VOLUME CAPACITY(26,1)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|CO2 EMISSION(23,2)\|TEMPERATURE GEOMEMBRANE(23,1)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|SOLUTION MINING(22,1)\|HYDROCARBONACEOUS MATERIAL(21,30)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|BRINE SOLUTION(21,1)\|ELECTROPLATING(21,1)\|EXTRACT FLUID(21,1)\|FLOTATION(19,1)\|IMPOUNDMENT WALL(18,12)\|LEACHING(18,1)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|GUIDELINE(17,4)\|REMOVING HYDROCARBON(16,6)\|BRINE(15,1)\|REFRACTORY CEMENT(13,4)\|SILICATE(13,4)\|BIOMASS(13,3)\|PRECIPITATION(13,3)\|SEALANT(13,2)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|ADDITIVE(12,13)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|GROUT(11,3)\|REBAR(11,3)\|DRAIN PIPE(11,1)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|MECHANICAL INTEGRITY(11,1)\|RESISTANCE HEATER(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|INFRASTRUCTURE OPERATING TEMPERATURE(10,1)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|EXTRACTION(9,2)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,11)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|VOID VOLUME(7,7)\|FUEL CELL(7,5)\|MATERIAL DEPOSITION(7,5)\|RADIO FREQUENCY(7,4)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ECONOMIC VALUE(7,1)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|ECONOMICALLY COMPETITIVE RECOVERY(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|LIQUID PRODUCT(5,11)\|PRECIOUS METAL(5,4)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|HYDROCARBON COMBUSTION(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HEATING RESIDENCE TIME(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PERMEABILITY BALANCE(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|HEAT TRANSFER(4,10)\|HYDROGEN DONOR(4,7)\|HEAVY METAL(4,4)\|BLASTING(4,3)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|ECONOMICS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|RECLAMATION(3,2)\|STOICHIOMETRIC CONDITION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|CO2 PRODUCTION(3,1)\|COAL CONTENT(3,1)\|COMMINUTED HYDRO CARBONACEOUS MATERIAL(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|FUTURE DATE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GASEOUS LIGHT HYDROCARBON(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HARVESTED HYDRO CARBONACEOUS MATERIAL(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|LONG HEATING RESIDENCE TIME(3,1)\|MICROBIOLOGY(3,1)\|MINED HYDRO CARBONACEOUS MATERIAL(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DIFFICULT CHALLENGE(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|FUNCTION VOID SPACE(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|\|(CN102395657)\|HYDROCARBONACEOUS MATERIAL(100,39)\|INFRASTRUCTURE(100,24)\|CONSTRUCTED PERMEABILITY(100,13)\|CARBON(100,6)\|HYDROCARBON RECOVERY(100,5)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|METHANEDIONE COLLECTION(48,4)\|METHANEDIONE(45,44)\|ECONOMICALLY COMPETITIVE RECOVERY(39,1)\|ENCAPSULATED VOLUME(31,18)\|METHANEDIONE PRECIPITATE(30,5)\|BENTONITE CLAY(30,1)\|SOLVENT RECOVERY(28,2)\|RESISTIVE HEATER(27,1)\|DEPLETED HYDROCARBONACEOUS MATERIAL(26,14)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(26,7)\|CLAY LINING(26,1)\|CONTROL INFRASTRUCTURE(23,27)\|LIQUID METHANEDIONE(23,13)\|IMPOUNDMENT(22,56)\|ION RESIN EXCHANGE(21,1)\|SYNTHETIC CLAY(21,1)\|INFRASTRUCTURE CONSTRUCTION(19,23)\|CRYOGENIC PRECIPITATION(19,2)\|DRAINAGE PIPE(19,2)\|ECONOMICS(19,1)\|TEMPERATURE GEOMEMBRANE(19,1)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(18,3)\|DIFFICULT CHALLENGE(18,1)\|AQUEOUS SOLUTION(17,10)\|UNDISTURBED GEOLOGICAL FORMATION(17,5)\|BRINE SOLUTION(17,1)\|ELECTROPLATING(17,1)\|SOLUTION MINING(17,1)\|UNDERGROUND MINING(17,1)\|PERMEABILITY(16,29)\|IMPOUNDMENT WALL(15,11)\|ASSURANCE(15,1)\|ENVIRONMENTAL HAZARD(15,1)\|FLOTATION(15,1)\|LEACHING(15,1)\|SEALANT(15,1)\|PERMEABILITY CONTROL IMPOUNDMENT(14,4)\|REMEDIATION(14,2)\|REMOVING HYDROCARBON(13,5)\|SEGMENTED CAPSULE IMPOUNDMENT(13,3)\|BRINE(12,3)\|CONVECTIVE HEATING(12,3)\|BLASTING(12,2)\|CAUSE UNDESIRABLE(12,1)\|FREEZE WALL(11,3)\|PRECIPITATION(11,3)\|RADIO FREQUENCY(11,3)\|REFRACTORY CEMENT(10,4)\|SILICATE(10,4)\|METHANEDIONE SEQUESTRATION(10,3)\|REMOVING PRODUCT(10,1)\|HEATED GAS(9,4)\|GRAVEL(9,3)\|GROUT(9,3)\|REBAR(9,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(9,1)\|CONVECTION(8,4)\|SUPERCRITICAL METHANEDIONE(8,2)\|ACID HALIDE(8,1)\|BIOCHEMICALLY OXIDIZE ORE(8,1)\|HYDROGEN CHLORIDE(8,1)\|MINE CAPSULE IMPOUNDMENT(8,1)\|UNDERGROUND FRESHWATER AQUIFER(8,1)\|MATERIAL DEPOSITION(7,3)\|AFT BERM PERMEABILITY(7,1)\|IMPOUNDMENT CONTAINMENT CAPSULE(7,1)\|HYDROCARBON PRODUCTION(6,11)\|IMPERMEABLE FLOOR(6,3)\|IMPERMEABLE SIDEWALL(6,2)\|NEARBY IMPOUNDMENT(6,2)\|TRILLION BARREL(6,2)\|BENTONITE AMENDED SOIL(6,1)\|ECONOMIC VALUE(6,1)\|SEQUESTERED METHANEDIONE(6,1)\|WOVEN BAMBOO BASKET(6,1)\|FUEL CELL(5,5)\|GUIDELINE(5,4)\|SOIL COMPACTION(5,3)\|MINED CRUSHED STONE(5,2)\|BIOEXTRACTION SCENARIO(5,1)\|CHALLENGING ENDEAVOR(5,1)\|COLLECTIVE IMPOUNDMENT(5,1)\|COMMINUTED AGGLOMERATE(5,1)\|DEEP SALINE AQUIFER(5,1)\|IMPOUNDMENT PERIMETER(5,1)\|INFRASTRUCTURE SHUTDOWN(5,1)\|LANDFILL IMPOUNDMENT(5,1)\|LEAK PROOF EXTRACTION IMPOUNDMENT(5,1)\|METHANE MOLECULE2MOLECULE(5,1)\|NANOCARBON FULLERENE(5,1)\|SEWAGE IMPOUNDMENT(5,1)\|SPRAYED CEMENT SLURRY(5,1)\|SUBDIVIDED IMPOUNDMENT(5,1)\|WATERPROOF QUALITY ENGINEERING(5,1)\|HEAT TRANSFER(4,11)\|LIQUID PRODUCT(4,11)\|GASEOUS PRODUCT(4,4)\|PRECIOUS METAL(4,4)\|IMPOUNDMENT HEIGHT(4,2)\|API MODIFIER(4,1)\|ATMOSPHERIC POLLUTANT(4,1)\|BRINE SATURATED ROCK FORMATION(4,1)\|CANADIAN TAR SAND(4,1)\|CARBONATE DECOMPOSITION(4,1)\|CEMENT REINFORCEMENT(4,1)\|COLLECTED METHANEDIONE(4,1)\|COMPACTED GEOGRID(4,1)\|CONDUIT STRUCTURING(4,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(4,1)\|CONTAINMENT BOUNDARY(4,1)\|CRANE SUSPENDED EXCAVATOR(4,1)\|CRUSHED ORE(4,1)\|DEBT PAYBACK(4,1)\|DECREASING HYDROGENATION(4,1)\|DIRTY FINE PARTICULATE(4,1)\|ECONOMIC VALUATION(4,1)\|EMPTY IMPOUNDMENT(4,1)\|ENGINEERED CARBON REINFORCED GRID(4,1)\|EXCAVATED CAVITY(4,1)\|FIXING METHANEDIONE(4,1)\|GASEOUS HYDROCARBON COMBUSTION HEATER(4,1)\|GEOLOGICAL RESERVOIR ANALYSIS(4,1)\|GEOSYNTHETIC FABRICS(4,1)\|GEOTEXTILE BAG(4,1)\|GRADE CEMENT SLURRY(4,1)\|GRAVITY ASSISTED DRAIN(4,1)\|GRAVITY DRAINAGE PROFILE(4,1)\|HYDROCARBON ENRICHMENT(4,1)\|HYDROCARBON EXCAVATED VOLUME(4,1)\|HYDROCARBON EXCAVATION(4,1)\|HYDROCARBON RICHNESS(4,1)\|HYDROCARBON UNCONTROLLED RELEASE(4,1)\|HYDROCARBONACEOUS DEPOSIT(4,1)\|IMPERMEABLE BARRIER ZONE(4,1)\|IMPERVIOUS BED(4,1)\|IMPOUNDMENT COLLECTION(4,1)\|IMPOUNDMENT FLOOR(4,1)\|IMPOUNDMENT SIDEWALL(4,1)\|INFRASTRUCTURE STABILIZATION(4,1)\|INJECTED CO2THE EFFECTIVE TRAPPING(4,1)\|INSULATION CONTAINMENT(4,1)\|MESSY DUMP(4,1)\|METHANEDIONE ABSORPTION(4,1)\|METHANEDIONE RESOLUTION(4,1)\|MINING AVOIDANCE(4,1)\|MINING HAUL TRUCK(4,1)\|NATIVE BACTERIA(4,1)\|NATURAL DISTRIBUTED COMBUSTOR(4,1)\|NEARBY INFRASTRUCTURE(4,1)\|NONCIRCULAR TUBING(4,1)\|ORE SOLVENT EXTRACTION(4,1)\|PILED RUBBLE(4,1)\|PILLAR MINING(4,1)\|PIT EXCAVATION(4,1)\|PLURAL REFERENT(4,1)\|REFORMING CATALYST(4,1)\|REFORMING ZONE(4,1)\|REGULATORY FLUID MIGRATION REGULATION(4,1)\|REINFORCED CEMENT(4,1)\|REMAINING SHALE DECREASING WETTABILITY(4,1)\|RESISTANT PVC LINER(4,1)\|SHALE MINING(4,1)\|SHELL ICP(4,1)\|SOIL AMENDMENT(4,1)\|SOY INSULATOR(4,1)\|STOICHIOMETRIC COMBUSTION(4,1)\|SUPER DISPOSITION(4,1)\|TAR SAND BITUMEN TREATMENT(4,1)\|TEXTURED BUILT TAIL(4,1)\|THERMALLY DETERIORATED WASTE SHALE(4,1)\|UNCOVERED CAPSULE(4,1)\|UNDERGROUND AQUIFER CONTAMINATION(4,1)\|UNDERGROUND RUBBLE CHANNEL(4,1)\|UNRECOVERED HYDROCARBON(4,1)\|UNUSED RESOURCE(4,1)\|WATERPROOF QUALITY INSULATION(4,1)\|WELLBORE DRILLING(4,1)\|HYDROGEN DONOR(3,7)\|CLAY(3,5)\|HEAVY METAL(3,5)\|MINED MATERIAL(3,5)\|ENZYME(3,4)\|AGITATION(3,3)\|BIOMASS(3,3)\|HEAT PIPE(3,3)\|LIGNITE(3,3)\|MINED HYDROCARBONACEOUS MATERIAL(3,3)\|PYROLYSIS(3,3)\|BIOREMEDIATION(3,2)\|FIXED STRUCTURE(3,2)\|GASEOUS LIGHT HYDROCARBON(3,2)\|HORIZONTAL MINING(3,2)\|OIL BLEND(3,2)\|UNCONTROLLED MIGRATION PREVENTION(3,2)\|ACCEPTED PIPELINE STANDARD(3,1)\|BUILT CAPSULE(3,1)\|CARBON REINFORCING GRID(3,1)\|CERMET COMPOSITE(3,1)\|COLLECTION TROUGH(3,1)\|CONSTRUCTED SULFUR CAPSULE(3,1)\|CONTAINMENT VESSEL SEGMENTATION(3,1)\|CONTAINMENT VESSEL STRUCTURE(3,1)\|DAMAGING STRESS(3,1)\|ECONOMIC FACTOR(3,1)\|EMBEDDED CONDUIT(3,1)\|ENHANCE COMPACTNESS(3,1)\|ENRICHMENT SENSOR(3,1)\|EXPLICITLY RECITED LIMIT(3,1)\|EXTRACTION CAPSULE TREATMENT ZONE(3,1)\|FLOOR LEVELING(3,1)\|FORMATION EXPERIMENTAL MODELING(3,1)\|GAS HEAT SOURCE(3,1)\|GEOPOLITICAL FACTOR(3,1)\|HYDROCARBON BEARING(3,1)\|IMPOUNDMENT DEPTH(3,1)\|IMPOUNDMENT LIFE SPAN(3,1)\|IMPOUNDMENT REGION(3,1)\|LEACHATE PRODUCTION(3,1)\|LEAK PROOF CONTAINMENT VESSEL(3,1)\|LOCALIZED HOTSPOT ELIMINATION(3,1)\|METALLIC ADDITIVE(3,1)\|METHANEDIONE PRODUCTION(3,1)\|MICROBIAL STRAIN(3,1)\|MINERAL LINER(3,1)\|MINING ORE GRADE(3,1)\|MOISTURE MIGRATION(3,1)\|ORE MOISTURE CONTENT(3,1)\|OUTER CAPSULE IMPOUNDMENT(3,1)\|PERFORATED HEATING PIPE(3,1)\|PERMEABILITY BARRIER(3,1)\|PERMEABLE PARTICLE(3,1)\|PIPE CONDENSER(3,1)\|PIPE PERFORATION(3,1)\|PREFABRICATED PIECE(3,1)\|PREFORMED PIECE(3,1)\|PROVEN RESERVOIR(3,1)\|RECOVERY STEAM(3,1)\|REDUCING CO2EMISSIONS(3,1)\|REFRACTORY CEMENT PIPE(3,1)\|REUSABLE PIPE(3,1)\|ROTARY RETORT(3,1)\|SPENT SHALE SOLID RINSING(3,1)\|STAGED CONTAINMENT VESSEL(3,1)\|STAGING PIPE(3,1)\|STORE METHANEDIONE(3,1)\|SUBTERRANEAN TREATMENT ZONE(3,1)\|SUPPLEMENTAL FUEL(3,1)\|SUPPORTIVE IMPOUNDMENT WALL FORMATION(3,1)\|SYNTHETIC GEOGRID(3,1)\|SYNTHETIC NANOCARBON(3,1)\|TAR SAND DEPOSIT(3,1)\|TOXIC EFFLUENT(3,1)\|TUNNELING(3,1)\|ULTRASONIC GENERATOR(3,1)\|VOLATILE HYDROCARBON(3,1)\|HEATING RATE(2,4)\|GEOLOGICAL FORMATION(2,3)\|HEATED FLUID(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|SILO(2,3)\|ADJACENT IMPOUNDMENT(2,2)\|ANCHOR MEMBER(2,2)\|ASPHALTENE(2,2)\|CATHETER(2,2)\|COMBUSTION EXHAUST GAS(2,2)\|COMPACTED FILL TOP(2,2)\|CRUSHING(2,2)\|CULLET(2,2)\|DETONATION(2,2)\|EXPLOSION(2,2)\|FIBERGLASS(2,2)\|HYDROCARBON LIQUID(2,2)\|HYDROGEN CONTENT(2,2)\|INVESTIGATION(2,2)\|POLYCARBONATE(2,2)\|PORTABLE COMBUSTION CHAMBER(2,2)\|RECIRCULATION(2,2)\|RECYCLING(2,2)\|STOICHIOMETRIC CONDITION(2,2)\|SWELLING(2,2)\|VAPOR PRODUCTION(2,2)\|ABUNDANT LIGHT HYDROCARBON(2,1)\|ACROSS MULTIPLE IMPOUNDMENT(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADVENT(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALONE MEET(2,1)\|AMBIENT ENVIRONMENT(2,1)\|ANAEROBIC CONDITION(2,1)\|ANCHOR PILE STRUCTURE(2,1)\|AQUEOUS MUD CONDITION(2,1)\|AROMATICS(2,1)\|ASSAYING(2,1)\|AVAILABLE ADDRESSING(2,1)\|BARRIER MANUFACTURE(2,1)\|BAUXITE(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOGLASS(2,1)\|BIOLEACHING(2,1)\|BITUMEN SOURCE(2,1)\|BLENDING KEROGEN OIL(2,1)\|BYPRODUCT(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPACITY INDICATOR(2,1)\|CATALYTIC GAS(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|CENTRAL GATHERING PIPE(2,1)\|CENTRAL RESERVOIR(2,1)\|CHROMATOGRAPHIC LOCATION(2,1)\|CO2AND(2,1)\|CO2CAN(2,1)\|COAL COMBINATION(2,1)\|COAL CONTENT(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPLEX MACHINERY(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|COMPUTER AIDED MINING(2,1)\|COMPUTER EQUIPMENT(2,1)\|CONCENTRATE(2,1)\|CONCRETE PANEL(2,1)\|CONDENSABILITY(2,1)\|CONDUCTIVE CEMENT(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED GEOMEMBRANE LAYER(2,1)\|CONSTRUCTED IMPOUNDMENT(2,1)\|CONSTRUCTED SULFUR CONTAINMENT VESSEL(2,1)\|CONTAINMENT CONSTRUCTION(2,1)\|CONTAINMENT DISPOSAL AREA(2,1)\|CONTAINMENT VESSEL CONSTRUCTION(2,1)\|CONTAINMENT VOLUME(2,1)\|CONTOUR(2,1)\|CONTROLLED QUALITY SHALE(2,1)\|COOLING FLUID(2,1)\|COOLING PIPE(2,1)\|CRUDE EXTRACTION(2,1)\|CURRENCY(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DEADMAN(2,1)\|DECREASING SULFUR(2,1)\|DECREASING VISCOSITY(2,1)\|DICTATION(2,1)\|DISPERSION FLUID SENSOR(2,1)\|DOWNWARDLY TRANSFERRED LIQUID(2,1)\|DUMPING(2,1)\|DUST PARTICLE(2,1)\|EARTH FORMATION(2,1)\|ECONOMICALLY VIABLE SOURCE(2,1)\|ELECTRICITY(2,1)\|ELECTROLYTE(2,1)\|ELEVATOR(2,1)\|ENCAPSULATED IMPOUNDMENT AREA(2,1)\|ENHANCE REMOVAL(2,1)\|ENHANCER(2,1)\|ENRICHED OIL BEARING ORE(2,1)\|ESTIMATE SOURCE(2,1)\|EXCAVATED HYDROCARBONACEOUS MATERIAL(2,1)\|EXCAVATION AREA(2,1)\|EXPOSED UNDISTURBED GROUND(2,1)\|EXTRACTION PORT(2,1)\|FAST RECOVERY(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE COLLECTION(2,1)\|FINE MESH(2,1)\|FLEXIBLE HOUSING(2,1)\|FLOOR CONSTRUCTION(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID EXTRACTION(2,1)\|FORSTERITE(2,1)\|FRACTURE(2,1)\|FRACTURING(2,1)\|FUNCTIONAL VOID SPACE(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS COMBUSTION(2,1)\|GAS GATHERING(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GAS RELEASE(2,1)\|GASEOUS HYDROCARBON PRODUCT(2,1)\|GEOLOGICAL LOCATION(2,1)\|GEOSYNTHETIC MEMBRANE(2,1)\|HALF ACRE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HAULING(2,1)\|HEAT ABSORPTION(2,1)\|HEATING CONDUIT COST(2,1)\|HEATING CONDUIT LOCATION(2,1)\|HEATING FLUID ISOLATION(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HORIZONTAL BOREHOLE(2,1)\|HOT GAS FILTRATION(2,1)\|HOTSPOT LOCALIZATION(2,1)\|HYDROCARBON VAPOR(2,1)\|HYDROCARBONACEOUS MATERIAL BIOHYDROXYLATION(2,1)\|HYDROCARBONACEOUS MATERIAL COMPACTION(2,1)\|HYDRODESULFURIZATION(2,1)\|HYDROTREAT(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE BOTTOM(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|INFRASTRUCTURE LOCATION(2,1)\|KEROGEN REMOVAL(2,1)\|LARGE CONTAINMENT IMPOUNDMENT(2,1)\|LAYER COMPACTION(2,1)\|LOCALIZED HEATING ZONE(2,1)\|METEOROLOGICAL DATA FACTOR(2,1)\|METHANE STORAGE(2,1)\|METHANEDIONE STORAGE(2,1)\|MINIMAL WASTE(2,1)\|MOLTEN CARBONATE FUEL CELL(2,1)\|MONITORING HEAT(2,1)\|NONHEATED BUFFER ZONE(2,1)\|NONHYDROCARBON(2,1)\|OIL SHALE ORE(2,1)\|OPEN ENDED CAPSULE IMPOUNDMENT(2,1)\|OPTIMIZATION REASON(2,1)\|ORGANIC ADDITIVE(2,1)\|PATHWAY(2,1)\|PIPELINE EXTENSION(2,1)\|PLANT FIBER CELLULOSE(2,1)\|POLYMERIC RESIN(2,1)\|PREVENT ACCIDENTAL LEACHING(2,1)\|PREVENTION MEASURE(2,1)\|PUMPING PIPE(2,1)\|RECOVERING OIL(2,1)\|RECOVERY TREATMENT(2,1)\|RECUPERATOR(2,1)\|REFORMATION(2,1)\|RELEVANT MEASUREMENT(2,1)\|RESIDUAL HYDROCARBON PRODUCT(2,1)\|RETURN DILUENT(2,1)\|ROUND TUBING(2,1)\|SAND PARTICLE(2,1)\|SEQUENTIAL SOLUTION RECOVERY(2,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(2,1)\|SOLVENT SUBSTITUTED COMPOUND(2,1)\|SPRAYED LIQUID EMULSION(2,1)\|STAGED PROCESSING(2,1)\|STEAM INJECTION(2,1)\|STEEL RETORT(2,1)\|STRUCTURED FEATURE(2,1)\|SUPPLEMENTAL HEATING(2,1)\|SUPPORTING BERMS(2,1)\|TECHNICAL CHALLENGE(2,1)\|TRANSFER DEFLATION(2,1)\|TRANSPORT CONDUIT(2,1)\|UNCONTROLLED ESCAPE PREVENTION(2,1)\|UPGRADING(2,1)\|VOLATILE ORGANIC(2,1)\|WATERTIGHT COVER(2,1)\|\|(AU2010213862)\|HYDROCARBONACEOUS MATERIAL(100,35)\|INFRASTRUCTURE(100,30)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDROCARBON RECOVERY(100,5)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|SEQUESTERING METHANEDIONE(66,1)\|METHANEDIONE COLLECTION(60,4)\|METHANEDIONE(51,48)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,22)\|CRYOGENIC PRECIPITATION(33,4)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(32,7)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(31,15)\|LIQUID METHANEDIONE(29,13)\|IMPOUNDMENT(27,53)\|CONTROL INFRASTRUCTURE(26,27)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|PERMEABILITY(20,24)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|REMOVING HYDROCARBON(16,6)\|SILICATE(13,4)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,10)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|MATERIAL DEPOSITION(7,5)\|BENTONITE CLAY(7,2)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|VOID VOLUME(5,4)\|GUIDELINE(5,3)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|LIQUID PRODUCT(4,10)\|HYDROGEN DONOR(4,6)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|CARBONATE DECOMPOSITION(4,1)\|CO2 EMISSION(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|HYDROCARBON COMBUSTION(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|ANTHEM DEGREE(3,2)\|BLASTING(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|PRECIPITATION(3,2)\|RECLAMATION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|COAL CONTENT(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|MICROBIOLOGY(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|VOID SPACE(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOOXIDATION(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ECONOMICS(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|EXCLUSION(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCLUSION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|LIMESTONE(2,1)\|LIMITED COMBUSTION INTENT(2,1)\|LIQUID CONDENSATION(2,1)\|LIQUID EMULSION(2,1)\|LIQUID SOLUTE(2,1)\|LUBRICANT COOLANT(2,1)\|\|(AU2010213862)\|HYDROCARBONACEOUS MATERIAL(100,35)\|INFRASTRUCTURE(100,30)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDROCARBON RECOVERY(100,5)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|SEQUESTERING METHANEDIONE(66,1)\|METHANEDIONE COLLECTION(60,4)\|METHANEDIONE(51,48)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,22)\|CRYOGENIC PRECIPITATION(33,4)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(32,7)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(31,15)\|LIQUID METHANEDIONE(29,13)\|IMPOUNDMENT(27,53)\|CONTROL INFRASTRUCTURE(26,27)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|PERMEABILITY(20,24)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|REMOVING HYDROCARBON(16,6)\|SILICATE(13,4)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,10)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|MATERIAL DEPOSITION(7,5)\|BENTONITE CLAY(7,2)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|VOID VOLUME(5,4)\|GUIDELINE(5,3)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|LIQUID PRODUCT(4,10)\|HYDROGEN DONOR(4,6)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|CARBONATE DECOMPOSITION(4,1)\|CO2 EMISSION(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|HYDROCARBON COMBUSTION(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|ANTHEM DEGREE(3,2)\|BLASTING(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|PRECIPITATION(3,2)\|RECLAMATION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|COAL CONTENT(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|MICROBIOLOGY(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|VOID SPACE(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOOXIDATION(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ECONOMICS(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|EXCLUSION(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCLUSION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|LIMESTONE(2,1)\|LIMITED COMBUSTION INTENT(2,1)\|LIQUID CONDENSATION(2,1)\|LIQUID EMULSION(2,1)\|LIQUID SOLUTE(2,1)\|LUBRICANT COOLANT(2,1)\|\|(IN1897/MUMNP/2011)\|HYDROCARBONACEOUS MATERIAL(100,35)\|INFRASTRUCTURE(100,25)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDROCARBON RECOVERY(100,5)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|METHANEDIONE COLLECTION(66,3)\|METHANEDIONE(54,50)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,21)\|CRYOGENIC PRECIPITATION(33,4)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(32,7)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(31,15)\|LIQUID METHANEDIONE(29,13)\|IMPOUNDMENT(27,52)\|CONTROL INFRASTRUCTURE(26,27)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|PERMEABILITY(19,23)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|REMOVING HYDROCARBON(16,6)\|SILICATE(13,4)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,10)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|MATERIAL DEPOSITION(7,5)\|BENTONITE CLAY(7,2)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|VOID VOLUME(5,4)\|GUIDELINE(5,3)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|LIQUID PRODUCT(4,10)\|HYDROGEN DONOR(4,6)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|CARBONATE DECOMPOSITION(4,1)\|CO2 EMISSION(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|HYDROCARBON COMBUSTION(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|BIOMASS(3,3)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|BLASTING(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|PRECIPITATION(3,2)\|RECLAMATION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|CO2 PRODUCTION(3,1)\|COAL CONTENT(3,1)\|COLLECTION UNIT OPERATIVE IY(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|MICROBIOLOGY(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|VOID SPACE(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ECONOMICS(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GEOMEMBRANE(2,1)\|GUARANTEE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|LIMESTONE(2,1)\|LIMITED COMBUSTION INTENT(2,1)\|LIQUID CONDENSATION(2,1)\|LIQUID EMULSION(2,1)\|LIQUID SOLUTE(2,1)\|LUBRICANT COOLANT(2,1)\|MATERIAL UNCONTROLLED MIGRATION(2,1)\|\|(CA2752524)\|HYDROCARBONACEOUS MATERIAL(100,36)\|INFRASTRUCTURE(100,25)\|CONSTRUCTED PERMEABILITY(100,13)\|HYDROCARBON RECOVERY(100,5)\|SEQUESTRATION(100,3)\|CARBON MANAGEMENT(100,2)\|METHANEDIONE EMISSION(100,2)\|SEQUESTERING METHANEDIONE EMISSION(100,2)\|ENCAPSULATED CONTROL INFRASTRUCTURE(100,1)\|METHANEDIONE COLLECTION(60,4)\|METHANEDIONE(54,49)\|METHANEDIONE PRECIPITATION(41,4)\|ENCAPSULATED VOLUME(38,22)\|CRYOGENIC PRECIPITATION(33,4)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(32,7)\|EXHAUSTED HYDROCARBONACEOUS MATERIAL(31,15)\|LIQUID METHANEDIONE(29,13)\|IMPOUNDMENT(27,54)\|CONTROL INFRASTRUCTURE(26,27)\|INFRASTRUCTURE CONSTRUCTION(23,22)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(22,4)\|AQUEOUS SOLUTION(21,10)\|UNDISTURBED GEOLOGICAL FORMATION(21,5)\|PERMEABILITY(20,24)\|PERMEABILITY CONTROL IMPOUNDMENT(17,5)\|REMOVING HYDROCARBON(16,6)\|SILICATE(13,4)\|SECTIONED CAPSULE IMPOUNDMENT(13,2)\|RECOVERING HYDROCARBON(11,7)\|COMPACTED FILL CEILING(11,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(11,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(11,1)\|UNDERGROUND FRESHWATER AQUIFER(11,1)\|HEAT PIPE(10,7)\|CONVECTION(10,4)\|METHANEDIONE PRECIPITATE(10,3)\|SUPERCRITICAL METHANEDIONE(10,2)\|QUARRY CAPSULE IMPOUNDMENT(10,1)\|UNCAPPED CAPSULE IMPOUNDMENT(10,1)\|UNDERGROUND RUBBLE CHIMNEY(10,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(9,1)\|NANOCARBON FULLERENE ADDITIVE(9,1)\|STRUCTURED IMPOUNDMENT CAPSULE(9,1)\|HYDROCARBON PRODUCTION(8,10)\|CONTAINMENT CAPSULE(8,2)\|NEARBY IMPOUNDMENT(8,2)\|TAILING BERM(8,2)\|UNRECOVERED HYDROCARBON(8,2)\|BENTONITE AMENDED SOIL(8,1)\|BITUMEN SIMULTANEOUS UPGRADING(8,1)\|MATERIAL DEPOSITION(7,5)\|BENTONITE CLAY(7,2)\|CAPSULE SECTION(7,2)\|HEATED GAS PASS(7,2)\|HYDROCARBON RICHNESS(7,2)\|ENGINEERED PERMEABILITY BARRIER(7,1)\|HYDROCARBON UNCONTROLLED EGRESS(7,1)\|SEQUESTERED METHANEDIONE(7,1)\|UNDERGROUND MINED HYDROCARBON(7,1)\|SALT WATER(6,6)\|BENCH MINING ELEVATION(6,1)\|BIOEXTRACTION SCENARIO(6,1)\|CHALLENGING ENDEAVOR(6,1)\|COLLECTIVE IMPOUNDMENT(6,1)\|DEEP SALINE AQUIFER(6,1)\|EXTERIOR CAPSULE IMPOUNDMENT(6,1)\|GARBAGE IMPOUNDMENT(6,1)\|GRAVITY ASSISTED DRAINAGE PIPE(6,1)\|GRAVITY DRAINAGE ASSISTANCE(6,1)\|INDISCRIMINATE DUMPING(6,1)\|INFRASTRUCTURE SHUTDOWN(6,1)\|MANIPULATED GRADE SHALE(6,1)\|METHANEDIONE ADSORPTION(6,1)\|PRECIPITATING METHANEDIONE(6,1)\|SEWAGE IMPOUNDMENT(6,1)\|SUBDIVIDED IMPOUNDMENT(6,1)\|UNTAPPED RESOURCE(6,1)\|WATERPROOF QUALITY ENGINEERING(6,1)\|VOID VOLUME(5,4)\|GUIDELINE(5,3)\|IMPERMEABLE FLOOR LAYER(5,3)\|CONSTRUCTED SULFUR CAPSULE(5,2)\|CORE DRILLING(5,2)\|IMPOUNDMENT HEIGHT(5,2)\|AB INITIO(5,1)\|ADDRESS METHANEDIONE(5,1)\|API MODIFIER(5,1)\|CANADIAN TAR SAND(5,1)\|CAPSULE SUBDIVISION(5,1)\|CEMENT FORTIFICATION(5,1)\|COLLECTED METHANEDIONE(5,1)\|COMPACTED GEOGRID(5,1)\|COMPACTED SOIL(5,1)\|COMPUTER ASSISTED MINING(5,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(5,1)\|CONTAINMENT BOUNDARY(5,1)\|CONVEYER RETRACTION(5,1)\|CRANE SUSPENDED EXCAVATOR(5,1)\|CRUSHED ORE(5,1)\|DESTINATION CAPSULE(5,1)\|DIRTY FINE PARTICULATE(5,1)\|ECONOMIC CONCERN(5,1)\|ECONOMIC VALUATION(5,1)\|EMPTY IMPOUNDMENT(5,1)\|ENGINEERED CARBON REINFORCEMENT GRID(5,1)\|EXCAVATED CAVITY(5,1)\|EXTRACTION IMPOUNDMENT(5,1)\|GEOPOLITICAL CONCERN(5,1)\|GEOSYNTHETIC FABRICS(5,1)\|GEOTEXTILE BAG(5,1)\|GOVERNMENT FLUID MIGRATION REGULATION(5,1)\|GRAVITY DRAINAGE CONTOUR(5,1)\|HEAT SOURCE GAS(5,1)\|HEATING MINED RUBBLE(5,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(5,1)\|HYDROLOGY MEASURE(5,1)\|IMPERMEABLE BARRIER ZONE(5,1)\|IMPORTED SAND(5,1)\|IMPOUNDMENT COLLECTION(5,1)\|IMPOUNDMENT FLOOR(5,1)\|IMPOUNDMENT OUTSIDE PERIMETER(5,1)\|INFRASTRUCTURE STABILIZATION(5,1)\|INTRINSIC PYROLYSIS(5,1)\|MICROORGANISM STRAIN(5,1)\|MINING QUARRY(5,1)\|NATIVE BACTERIA(5,1)\|NATURAL DISTRIBUTED COMBUSTOR(5,1)\|NEARBY INFRASTRUCTURE(5,1)\|NONCIRCULAR CONDUIT(5,1)\|NONPERMEABLE INSULATION(5,1)\|ORE SOLVENT EXTRACTION(5,1)\|PILED RUBBLE(5,1)\|PILLAR MINING(5,1)\|PIT EXCAVATION(5,1)\|PORTABLE COMBUSTOR(5,1)\|PREFORMED PIECE STACKING(5,1)\|REFORMING CATALYST(5,1)\|REFORMING ZONE(5,1)\|REINFORCED CEMENT(5,1)\|RESISTANT PVC LINER(5,1)\|RETURNING DILUENT ELIMINATION(5,1)\|SOIL AMENDMENT(5,1)\|SPRAYABLE REFRACTORY(5,1)\|SPRAYED GROUTING(5,1)\|STEEL FABRICATED RETORT(5,1)\|STEPPED DOWNSLOPE(5,1)\|STOICHIOMETRIC COMBUSTION(5,1)\|SUPER DISPOSITION(5,1)\|TAR SAND BITUMEN TREATMENT(5,1)\|TRILLION BARREL(5,1)\|UNCOVERED CAPSULE(5,1)\|UNDERGROUND AQUIFER CONTAMINATION(5,1)\|LIQUID PRODUCT(4,10)\|HYDROGEN DONOR(4,6)\|FIBERGLASS(4,3)\|FREEZE WALL(4,3)\|LIGNITE(4,3)\|CONVECTIVE HEATING(4,2)\|CRUSHED GLASS(4,2)\|FIXED STRUCTURE(4,2)\|FLOOR CONSTRUCTION(4,2)\|HEATED CONDUIT(4,2)\|HORIZONTAL MINING(4,2)\|ACCEPTED PIPELINE STANDARD(4,1)\|AQUATHERMAL REACTION(4,1)\|BARRIER INSULATION(4,1)\|CAP BARRIER ZONE(4,1)\|CARBONATE DECOMPOSITION(4,1)\|COMPLICATED MACHINERY(4,1)\|DAMAGING STRESS(4,1)\|EGRESS EXIT(4,1)\|ELECTRICAL RESISTIVE HEATER(4,1)\|EMBEDDED CONDUIT(4,1)\|ENHANCE COMPACTION(4,1)\|ENHANCING BITUMEN REMOVAL(4,1)\|EXPLICITLY RECITED LIMIT(4,1)\|FILL COMPACTION(4,1)\|FLOOR LEVELING(4,1)\|GASEOUS PRODUCT MINIMIZATION(4,1)\|GEOLOGICAL RESERVE ANALYSIS(4,1)\|GLOBAL WARMING CONCERN(4,1)\|HYDROCARBON COMBUSTION(4,1)\|IMPOUNDMENT DEPTH(4,1)\|IMPOUNDMENT REGION(4,1)\|ISOLATED CAPSULE(4,1)\|LEACHATE PRODUCTION(4,1)\|LIBERATED GASEOUS PRODUCT(4,1)\|LOCALIZED HOTSPOT ELIMINATION(4,1)\|METHANE STORE(4,1)\|METHANEDIONE STORAGE(4,1)\|MINERAL LINER(4,1)\|MINING ORE GRADE(4,1)\|MOISTURE MIGRATION(4,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(4,1)\|ORE MOISTURE CONTENT(4,1)\|PERMEABILITY PARTICLE(4,1)\|PIPE PERFORATION(4,1)\|PLENTIFUL LIGHT HYDROCARBON(4,1)\|POLYMERIC REFUSE(4,1)\|REFRACTORY CEMENT PIPE(4,1)\|REUSABLE PIPE(4,1)\|RICHNESS SENSOR(4,1)\|SOIL COMPACTION(4,1)\|SOY INSULATION(4,1)\|SPENT SHALE SOLID RINSING(4,1)\|STRATOGRAPHIC LOCATION(4,1)\|SUPPLEMENTAL FUEL(4,1)\|SWELLING BEHAVIOR(4,1)\|SYNTHETIC GEOGRID(4,1)\|SYNTHETIC NANO CARBON(4,1)\|TAR SAND DEPOSIT(4,1)\|TOXIC EFFLUENT(4,1)\|ULTRASONIC GENERATOR(4,1)\|UNDISTURBED SOIL(4,1)\|VOLATILE HYDROCARBON(4,1)\|WATERTIGHT CAP(4,1)\|KEROGEN OIL(3,4)\|HEATED FLUID(3,3)\|PIPING(3,3)\|VAPOR PRODUCTION(3,3)\|ACRE(3,2)\|ADJACENT IMPOUNDMENT(3,2)\|AGITATION(3,2)\|AIR EMISSION(3,2)\|ANCHOR MEMBER(3,2)\|BLASTING(3,2)\|CAPSULE WALL(3,2)\|CRUSHING(3,2)\|EXPLOSION(3,2)\|GABION(3,2)\|GEOMEMBRANE(3,2)\|HAULING(3,2)\|HYDROGEN CONTENT(3,2)\|INNER CAPSULE(3,2)\|INVESTIGATION(3,2)\|POLYCARBONATE(3,2)\|PRECIPITATION(3,2)\|RECLAMATION(3,2)\|ANAEROBIC CONDITION(3,1)\|AQUEOUS SLURRY(3,1)\|BARRIER MANUFACTURE(3,1)\|BRINE SATURATED ROCK FORMATION(3,1)\|CAPACITY INDICATOR(3,1)\|CAPSULE IMPOUNDMENT AREA(3,1)\|CATALYZING GAS(3,1)\|CEILING CAP(3,1)\|CLAY PIPE(3,1)\|COAL CONTENT(3,1)\|COMMINUTED MASS(3,1)\|COMPOSITION ADMIXTURE(3,1)\|CONCRETE PANEL(3,1)\|CONDUCTIVE CEMENT(3,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(3,1)\|CONSTRUCTED IMPOUNDMENT(3,1)\|DECREASED VISCOSITY(3,1)\|DISPERSION FLUID SENSOR(3,1)\|DUST PARTICLE(3,1)\|ECONOMICALLY VIABLE SOURCE(3,1)\|FAST RECOVERY(3,1)\|FINE COLLECTION(3,1)\|FLUID DRAINAGE(3,1)\|GAS COMBUSTION HEATER(3,1)\|GASEOUS HYDROCARBON PRODUCT(3,1)\|GEO MEMBRANE LAYER(3,1)\|GEO SYNTHETIC MEMBRANE(3,1)\|GEOLOGICAL LOCATION(3,1)\|HEATING CONDUIT PLACEMENT(3,1)\|HOTSPOT LOCALIZATION(3,1)\|HYDROCARBON VAPOR(3,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(3,1)\|HYDRODESULFURIZATION(3,1)\|IMMOBILIZATION(3,1)\|IMPOUNDMENT USEFUL LIFE(3,1)\|INJECTED CO2(3,1)\|KEROGEN REMOVAL(3,1)\|LAYER COMPACTION(3,1)\|MICROBIOLOGY(3,1)\|MINIMAL WASTE(3,1)\|MINING HAUL TRUCK NEED(3,1)\|MOLTEN CARBONATE FUEL CELL(3,1)\|MONITORING HEAT(3,1)\|NONHEATED BUFFER ZONE(3,1)\|OIL BLEND(3,1)\|OPTIMIZATION REASON(3,1)\|ORGANIC ADDITIVE(3,1)\|PIPELINE EXTENSION(3,1)\|PLANT FIBER CELLULOSE(3,1)\|POLYMERIC RESIN(3,1)\|PRECAST PIECE(3,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(3,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(3,1)\|QUALITY DETERIORATION(3,1)\|RECOVERED HYDROCARBON LIQUID(3,1)\|RECOVERING OIL(3,1)\|REFORMATION(3,1)\|RESIDUAL HYDROCARBON PRODUCT(3,1)\|RESIDUAL SHALE REDUCED WETTING(3,1)\|RICH OIL BEARING ORE(3,1)\|ROTATING RETORT(3,1)\|SAND PARTICLE(3,1)\|SEQUENTIAL SOLUTION RECOVERY(3,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(3,1)\|SOLVENT SUBSTITUTED COMPOUND(3,1)\|STAGED PROCESSING(3,1)\|STEAM INJECTION(3,1)\|TECHNICAL CHALLENGE(3,1)\|TREMENDOUS VOLUME(3,1)\|UNCONTROLLED ESCAPE PREVENTION(3,1)\|UNCONTROLLED MIGRATION PREVENTION(3,1)\|VARIED ENZYME(3,1)\|VOLATILE ORGANIC(3,1)\|HEATING RATE(2,3)\|INJECTION RATE(2,3)\|PEAT(2,3)\|PROPANE(2,3)\|RECOVERY(2,3)\|VOID SPACE(2,3)\|ADDED PERMEABILITY(2,1)\|ADJACENT INFRASTRUCTURE(2,1)\|ADJACENT NONHYDROCARBON(2,1)\|AGGLOMERATION(2,1)\|AGGREGATE PRODUCTION(2,1)\|ALKENE(2,1)\|ALLOY CONSTRUCTION(2,1)\|ASPHALTENE(2,1)\|AVAILABLE ADDRESSING(2,1)\|BAUXITE(2,1)\|BERM SUPPORT(2,1)\|BINDER(2,1)\|BIOCATALYST(2,1)\|BIOLEACHING(2,1)\|BIOMATERIAL(2,1)\|BIOOXIDATION(2,1)\|BIOREACTION(2,1)\|BIORECOVERY(2,1)\|BITUMEN SOURCE(2,1)\|CALCINED PETROLEUM COKE(2,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(2,1)\|CATALYTICALLY ACTIVE METAL(2,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(2,1)\|COMPOSITE WALL(2,1)\|COMPOUND SUBSTITUTION(2,1)\|CONDENSABILITY(2,1)\|CONDUIT PASS(2,1)\|CONDUIT WALL(2,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(2,1)\|COOLING PIPE(2,1)\|CYCLOHEXANE(2,1)\|CYCLOPENTANE(2,1)\|DANGER REDUCTION(2,1)\|DIFFERING LAYER(2,1)\|DISCHARGE PIPE(2,1)\|DISPERSION RATE(2,1)\|DOWN CHUTE(2,1)\|DRAINPIPE(2,1)\|ECONOMICS(2,1)\|ELECTRICITY(2,1)\|ELECTROLYSIS(2,1)\|EMBANKMENT(2,1)\|ENCLOSED VOLUME(2,1)\|ENVIRONMENTAL STEWARDSHIP(2,1)\|EXCAVATION AREA(2,1)\|FINAL HYDROCARBON PRODUCT(2,1)\|FINAL PRODUCT RECOVERY(2,1)\|FINE MESH(2,1)\|FLUID COMMUNICATION(2,1)\|FLUID DELIVERY(2,1)\|FLUID EXTRACTION(2,1)\|FLUIDITY(2,1)\|FORSTERITE(2,1)\|FOUNDATION(2,1)\|FRACTURING(2,1)\|FREEDOM(2,1)\|GAS BARRIER(2,1)\|GAS COLLECTION OUTLET(2,1)\|GAS GATHERING(2,1)\|GAS INGRESS(2,1)\|GAS INJECTION(2,1)\|GAS MIGRATION(2,1)\|GUARANTEE(2,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(2,1)\|HEATING OIL SHALE(2,1)\|HEATING SERVICE(2,1)\|HEAVY OIL RECYCLING(2,1)\|HOLDING TANK PROXIMITY(2,1)\|HOT GAS FILTERING(2,1)\|HYDROCARBON FLUID(2,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(2,1)\|HYDROGENATION(2,1)\|IMPERMEABILITY(2,1)\|IMPERMEABLE LAYER(2,1)\|IMPERMEABLE WALL(2,1)\|IMPERVIOUS LAYER(2,1)\|IMPOUNDMENT SIZE(2,1)\|IMPOUNDMENT WALL CONSTRUCTION(2,1)\|INCORPORATION(2,1)\|INDIGENOUS PLANT(2,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(2,1)\|LANGUAGE(2,1)\|LAYER CONDUIT(2,1)\|LAYING WIRE(2,1)\|LIGHTER(2,1)\|LIMESTONE(2,1)\|LIMITED COMBUSTION INTENT(2,1)\|LIQUID CONDENSATION(2,1)\|LIQUID EMULSION(2,1)\|LIQUID SOLUTE(2,1)\|LUBRICANT COOLANT(2,1)\|MATERIAL UNCONTROLLED MIGRATION(2,1)\|	(US8323481)\|What is claimed is:\|1. A method of sequestering carbon dioxide emissions during recovery of hydrocarbons from hydrocarbonaceous materials comprising:\| a) forming a constructed permeability control infrastructure which defines a substantially encapsulated volume, said infrastructure comprising clay, bentonite clay, bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, engineered cementitious composites (ECC), fiber reinforced composites, geosynthetic fabrics, sealant, grout, compacted earth, low grade shale, or combinations thereof, wherein the control infrastructure is formed in direct contact with walls of an excavated hydrocarbonaceous material deposit or is freestanding having either a foundation support of earthen material or a local surface topography as a floor;\| b) introducing a comminuted hydrocarbonaceous material into the control infrastructure to form a permeable body of hydrocarbonaceous material;\| c) heating the permeable body sufficient to remove hydrocarbons therefrom such that the hydrocarbonaceous material is substantially stationary during heating;\| d) sequestering carbon dioxide produced during the heating; and e) collecting the removed hydrocarbons.\|2. The method of claim 1, wherein sequestering carbon dioxide is achieved by reacting carbon dioxide with an aqueous solution to form a precipitation of carbon dioxide with a metal.\|3. The method of claim 2, wherein the metal is selected from the group consisting of calcium, magnesium, oxides thereof, silicates thereof, and mixtures thereof.\|4. The method of claim 2, wherein the aqueous solution is salt water.\|5. The method of claim 1, wherein sequestering carbon dioxide is achieved by injecting exhausted hydro carbonaceous materials with the carbon dioxide and salt water.\|6. The method of claim 1, wherein sequestering carbon dioxide is achieved by cryogenic precipitation forming liquid carbon dioxide.\|7. The method of claim 6, wherein the liquid carbon dioxide is mixed with exhausted hydrocarbonaceous materials.\|8. The method of claim 1, wherein sequestering carbon dioxide is achieved by injecting exhausted hydrocarbonaceous materials with the carbon dioxide.\|9. The method of claim 8, wherein the injecting is performed with a catalyst.\|10. The method of claim 1, wherein the step of heating includes injecting heated gases into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body.\|11. The method of claim 1, wherein the permeable body further comprises a plurality of conduits embedded within the permeable body, at least some of said conduits being configured as heating pipes.\|12. The method of claim 1, wherein the infrastructure comprises clay, bentonite clay, bentonite amended soil, compacted fill, compacted earth, low grade shale, or combinations thereof.	(US8323481)\|RELATED APPLICATION\|[0001] This application claims priority to U.S. Provisional Patent Application No. 61/152,220 filed Feb. 12, 2009 which is incorporated herein by reference.\|(US8323481)\|BACKGROUND\|[0002] Global and domestic demand for fossil fuels continues to rise despite price increases and other economic and geopolitical concerns. As such demand continues to rise, research and investigation into finding additional economically viable sources of fossil fuels correspondingly increases. Historically, many have recognized the vast quantities of energy stored in oil shale, coal and tar sand deposits, for example. However, these sources remain a difficult challenge in terms of economically competitive recovery. Canadian tar sands have shown that such efforts can be fruitful, although many challenges still remain, including environmental impact, product quality, production costs and process time, among others.\|[0003] Estimates of world-wide oil shale reserves range from two to almost seven trillion barrels of oil, depending on the estimating source. Regardless, these reserves represent a tremendous volume and remain a substantially untapped resource. A large number of companies and investigators continue to study and test methods of recovering oil from such reserves. In the oil shale industry, methods of extraction have included underground rubble chimneys created by explosions, in-situ methods such as In-Situ Conversion Process (ICP) method (Shell Oil), and heating within steel fabricated retorts. Other methods have included in-situ radio frequency methods (microwaves), and “modified” in-situ processes wherein underground mining, blasting and retorting have been combined to make rubble out of a formation to allow for better heat transfer and product removal.\|[0004] Among typical oil shale processes, all face tradeoffs in economics and environmental concerns. No current process alone satisfies economic, environmental, and technical challenges. Moreover, global warming concerns give rise to additional measures to address carbon dioxide (CO2) emissions which are associated with such processes. Methods are needed that accomplish environmental stewardship, yet still provide high-volume cost-effective oil production.\|[0005] Below ground in-situ concepts emerged based on their ability to produce high volumes while avoiding the cost of mining. While the cost savings resulting from avoiding mining can be achieved, the in-situ method requires heating a formation for a longer period of time due to the extremely low thermal conductivity and high specific heat of solid oil shale. Perhaps the most significant challenge for any in-situ process is the uncertainty and long term potential of water contamination that can occur with underground freshwater aquifers. In the case of Shell's ICP method, a “freeze wall” is used as a barrier to keep separation between aquifers and an underground treatment area. Although this is possible, no long term analysis has proven for extended periods to guarantee the prevention of contamination. Without guarantees and with even fewer remedies should a freeze wall fail, other methods are desirable to address such environmental risks.\|[0006] For this and other reasons, the need remains for methods and systems which can provide improved recovery of hydrocarbons from suitable hydrocarbon-containing materials, which have acceptable economics and avoid the drawbacks mentioned above.\|SUMMARY\|[0007] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating the hydrocarbonaceous material can be substantially stationary. Additionally, during heating, any carbon dioxide that is produced can be sequestered. Removed hydrocarbons can be collected for further processing, use in the process as supplemental fuel or additives, and/or direct use without further treatment.\|[0008] Additional features and advantages of these principles will be apparent from the following detailed description, which illustrates, by way of example, features of the invention.\|(US8323481)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0009] FIG. 1 is side partial cutaway view schematic of a constructed permeability control infrastructure in accordance with one embodiment.\|[0010] FIGS. 2A and 2B are top and plan views of a plurality of permeability control impoundments in accordance with one embodiment.\|[0011] FIG. 3 is a side cutaway view of a permeability control impoundment in accordance with one embodiment.\|[0012] FIG. 4 is a schematic of a portion of a constructed infrastructure in accordance with an embodiment.\|[0013] FIG. 5 is a schematic showing heat transfer between two permeability control impoundments in accordance with another embodiment.\|(US8323481)\|DETAILED DESCRIPTION\|[0014] It should be noted that the figures are merely exemplary of several embodiments and no limitations on the scope of the present invention are intended thereby. Further, the figures are generally not drawn to scale, but are drafted for purposes of convenience and clarity in illustrating various aspects of the invention.\|DETAILED DESCRIPTION\|[0015] Reference will now be made to exemplary embodiments and specific language will be used herein to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended. Alterations and further modifications of the inventive features described herein, and additional applications of the principles of the invention as described herein, which would occur to one skilled in the relevant art and having possession of this disclosure, are to be considered within the scope of the invention. Further, before particular embodiments are disclosed and described, it is to be understood that this invention is not limited to the particular process and materials disclosed herein as such may vary to some degree. It is also to be understood that the terminology used herein is used for the purpose of describing particular embodiments only and is not intended to be limiting, as the scope of the present invention will be defined only by the appended claims and equivalents thereof.\|DEFINITIONS\|[0016] In describing and claiming the present invention, the following terminology will be used.\|[0017] The singular forms “a,” “an,” and “the” include plural references unless the context clearly dictates otherwise. Thus, for example, reference to “a wall” includes reference to one or more of such structures, “a permeable body” includes reference to one or more of such materials, and “a heating step” refers to one or more of such steps.\|[0018] As used herein “existing grade” or similar terminology refers to the grade or a plane parallel to the local surface topography of a site containing an infrastructure as described herein which infrastructure may be above or below the existing grade.\|[0019] As used herein, “conduits” refers to any passageway along a specified distance which can be used to transport materials and/or heat from one point to another point. Although conduits can generally be circular pipes, other non-circular conduits can also be useful. Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|[0020] As used herein, “constructed infrastructure” refers to a structure which is substantially entirely man made, as opposed to freeze walls, sulfur walls, or other barriers which are formed by modification or filling pores of an existing geological formation.\|[0021] The constructed permeability control infrastructure is often substantially free of undisturbed geological formations, although the infrastructure can be formed adjacent or in direct contact with an undisturbed formation. Such a control infrastructure can be unattached or affixed to an undisturbed formation by mechanical means, chemical means, or a combination of such means, e.g. bolted into the formation using anchors, ties, or other suitable hardware.\|[0022] As used herein, “comminuted” refers to breaking a formation or larger mass into pieces. A comminuted mass can be rubbilized or otherwise broken into fragments.\|[0023] As used herein, “hydrocarbonaceous material” refers to any hydrocarbon-containing material from which hydrocarbon products can be extracted or derived. For example, hydrocarbons may be extracted directly as a liquid, removed via solvent extraction, directly vaporized or otherwise removed from the material. However, many hydro carbonaceous materials contain kerogen or bitumen which is converted to a hydrocarbon through heating and pyrolysis. Hydrocarbonaceous materials can include, but is not limited to, oil shale, tar sands, coal, lignite, bitumen, peat, and other organic materials.\|[0024] As used herein, “impoundment” refers to a structure designed to hold or retain an accumulation of fluid and/or solid moveable materials. An impoundment generally derives at least a substantial portion of foundation and structural support from earthen materials. Thus, the control walls do not always have independent strength or structural integrity apart from the earthen material and/or formation against which they are formed.\|[0025] As used herein, “permeable body” refers to any mass of comminuted hydro carbonaceous material having a relatively high permeability which exceeds permeability of a solid undisturbed formation of the same composition. Suitable permeable bodies can have greater than about 10% void space and typically have void space from about 30% to 45%, although other ranges may be suitable. Allowing for high permeability facilitates, for example, through the incorporation of large irregularly shaped particles, heating of the body through convection as the primary heat transfer while also substantially reducing costs associated with crushing to very small sizes, e.g. below about 1 to about 0.5 inch.\|[0026] As used herein, “wall” refers to any constructed feature having a permeability control contribution to confining material within an encapsulated volume defined at least in part by control walls. Walls can be oriented in any manner such as vertical, although ceilings, floors, and other contours defining the encapsulated volume can also be “walls” as used herein.\|[0027] As used herein, “mined” refers to a material which has been removed or disturbed from an original stratographic or geological location to a second and different location or returned to the same location. Typically, mined material can be produced by rubbilizing, crushing, explosively detonating, or otherwise removing material from a geologic formation.\|[0028] As used herein, “adsorb,” “adsorbing,” or “adsorbed” refers to the process where a gas or liquid solute accumulates on the surface of a solid or a liquid or diffuses into a solid or liquid. Generally, when referring to carbon dioxide, the carbon dioxide is adsorbed into a material such that the carbon dioxide is substantially immobilized.\|[0029] As used herein, “substantially stationary” refers to nearly stationary positioning of materials with a degree of allowance for subsidence, expansion, and/or settling as hydrocarbons are removed from the hydrocarbonaceous material from within the enclosed volume to leave behind lean material. In contrast, any circulation and/or flow of hydrocarbonaceous material such as that found in fluidized beds or rotating retorts involves highly substantial movement and handling of hydrocarbonaceous material.\|[0030] As used herein, “substantial” when used in reference to a quantity or amount of a material, or a specific characteristic thereof, refers to an amount that is sufficient to provide an effect that the material or characteristic was intended to provide. The exact degree of deviation allowable may in some cases depend on the specific context. Similarly, “substantially free of” or the like refers to the lack of an identified element or agent in a composition. Particularly, elements that are identified as being “substantially free of” are either completely absent from the composition, or are included only in amounts which are small enough so as to have no measurable effect on the composition.\|[0031] As used herein, “about” refers to a degree of deviation based on experimental error typical for the particular property identified. The latitude provided the term “about” will depend on the specific context and particular property and can be readily discerned by those skilled in the art. The term “about” is not intended to either expand or limit the degree of equivalents which may otherwise be afforded a particular value. Further, unless otherwise stated, the term “about” shall expressly include “exactly,” consistent with the discussion below regarding ranges and numerical data.\|[0032] Concentrations, dimensions, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of about 1 to about 200 should be interpreted to include not only the explicitly recited limits of 1 and 200, but also to include individual sizes such as 2, 3, 4, and sub-ranges such as 10 to 50, 20 to 100, etc.\|[0033] As used herein, a plurality of items, structural elements, compositional elements, and/or materials may be presented in a common list for convenience. However, these lists should be construed as though each member of the list is individually identified as a separate and unique member. Thus, no individual member of such list should be construed as a de facto equivalent of any other member of the same list solely based on their presentation in a common group without indications to the contrary.\|[0034] Carbon Management and Sequestration from Control Infrastructures\|[0035] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined or harvested hydro carbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure is a fixed structure. Additionally, during heating, at least a portion of carbon dioxide that is produced can be sequestered. Removed fluid hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.\|[0036] The constructed permeability control infrastructure can be formed using existing grade as floor support and/or as side wall support for the constructed infrastructure. For example, the control infrastructure can be formed as a free standing structure, i.e. using only existing grade as a floor with side walls being man-made. Alternatively, the control infrastructure can be formed within an excavated pit. Regardless, the control infrastructures are always formed above-grade.\|[0037] A constructed permeability control infrastructure can include a permeability control impoundment which defines a substantially encapsulated volume. The permeability control impoundment is substantially free of undisturbed geological formations. Specifically, the permeability control aspect of the impoundment can be completely constructed and manmade as a separate isolation mechanism for prevention of uncontrolled migration of material into or out of the encapsulated volume.\|[0038] In one embodiment, the permeability control impoundment can be formed along walls of an excavated hydrocarbonaceous material deposit. For example, oil shale, tar sands, or coal can be mined from a deposit to form a cavity which corresponds approximately to a desired encapsulation volume for an impoundment. The excavated cavity can then be used as a form and support to create the permeability control impoundment.\|[0039] In one alternative aspect, at least one additional excavated hydrocarbonaceous material deposit can be formed such that a plurality of impoundments can be operated. Further, such a configuration can facilitate a reduction in transportation distance of the mined material. Specifically, the mined hydro carbonaceous material for any particular encapsulated volume can be mined from an adjacent excavated hydrocarbonaceous material deposit. In this manner, a grid of constructed structures can be built such that mined material can be immediately and directly filled into an adjacent impoundment.\|[0040] Mining and/or excavation of hydrocarbonaceous deposits can be accomplished using any suitable technique. Conventional surface mining can be used, although alternative excavators can also be used without requirement of transportation of the mined materials. In one specific embodiment, the hydrocarbonaceous deposit can be excavated using a crane-suspended excavator. One example of a suitable excavator can include vertical tunnel boring machines. Such machines can be configured to excavate rock and material beneath the excavator. As material is removed, the excavator is lowered to ensure substantially continuous contact with a formation. Removed material can be conveyed out of the excavation area using conveyors or lifts. Alternatively, the excavation can occur under aqueous slurry conditions to reduce dust problems and act as a lubricant/coolant. The slurry material can be pumped out of the excavation for separation of solids in a settling tank or other similar solid-liquid separator, or the solids may be allowed to precipitate directly in an impoundment. This approach can be readily integrated with simultaneous or sequential solution-based recovery of metals and other materials as described in more detail below.\|[0041] Further, excavation and formation of a permeability control impoundment can be accomplished simultaneously. For example, an excavator can be configured to remove hydrocarbonaceous material while side walls of an impoundment are formed. Material can be removed from just underneath edges of the side walls such that the walls can be guided downward to allow additional wall segments to be stacked above. This approach can allow for increased depths while avoiding or reducing dangers of cave-in prior to formation of supporting impoundment walls.\|[0042] The impoundment can be formed of any suitable material which provides isolation of material transfer across walls of the impoundment. In this manner, integrity of the walls is retained during operation of the control infrastructure sufficient to substantially prevent uncontrolled migration of fluids outside of the control infrastructure. Non-limiting examples of suitable material for use in forming the impoundment of the constructed permeability control infrastructure can include clay, bentonite clay (e.g. clay comprising at least a portion of bentonite), bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, or combinations thereof. Engineered cementitious composites (ECC) materials, fiber reinforced composites, and the like can be particularly strong and can be readily engineered to meet permeability and temperature tolerance requirements of a given installation. As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required. For example, materials having a melting point above the maximum operating temperature of the infrastructure can be useful to maintain containment during and after heating and recovery. However, lower temperature materials can also be used if a non-heated buffer zone is maintained between the walls and heated portions of the permeable body. Such buffer zones can range from 6 inches to 50 feet depending on the particular material used for the impoundment and the composition of the permeable body. In another aspect, walls of the impoundment can be acid, water, and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water. For impoundment walls formed along formations or other solid support, the impoundment walls can be formed of a sprayed grouting, sprayed liquid emulsions, or other sprayed material such as sprayable refractory grade grouting which forms a seal against the formation and creates the permeability control wall of the impoundments. Impoundment walls may be substantially continuous such that the impoundment defines the encapsulated volume sufficiently to prevent substantial movement of fluids into or out of the impoundment other than defined inlets and outlets, e.g. via conduits or the like as discussed herein. In this manner, the impoundments can readily meet government fluid migration regulations. Alternatively, or in combination with a manufactured barrier, portions of the impoundment walls can be undisturbed geological formation and/or compacted earth. In such cases, the constructed permeability control infrastructure is a combination of permeable and impermeable walls as described in more detail below.\|[0043] In one detailed aspect, a portion of hydro carbonaceous material, either pre- or post-processed, can be used as a cement fortification and/or cement base which are then poured in place to form portions or the entirety of walls of the control infrastructure. These materials can be formed in place or can be preformed and then assembled on site to form an integral impoundment structure. For example, the impoundment can be constructed by cast forming in place as a monolithic body, extrusion, stacking of preformed or precast pieces, concrete panels joined by a grout (cement, ECC, or other suitable material), inflated form, or the like. The forms can be built up against a formation or can be stand alone structures. Forms can be constructed of any suitable material such as, but not limited to, steel, wood, fiberglass, polymer, or the like. The forms can be assembled in place or may be oriented using a crane or other suitable mechanism. Alternatively, the constructed permeability control infrastructure can be formed of gabions and/or geosynthetic fabrics assembled in layers with compacted fill material. Optional binders can be added to enhance compaction of the permeability control walls. In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|[0044] Impoundment walls can optionally include non-permeable insulation and/or fines collection layers. These permeable layers can be oriented between the permeability control barrier and the permeable body. For example, a layer of hydrocarbonaceous comminuted material can be provided which allows fluids to enter, cool, and at least partially condense within the layer. Such permeable layer material can generally have a particle size smaller than the permeable body. Further, such hydrocarbonaceous material can remove fines from passing fluids via various attractive forces. In one embodiment, the construction of impoundment walls and floors can include multiple compacted layers of indigenous or manipulated low grade shale with any combination of sand, cement, fiber, plant fiber, nano carbons, crushed glass, reinforcement steel, engineered carbon reinforcement grid, calcium salts, and the like. In addition to such composite walls, designs which inhibit long term fluid and gas migration through additional impermeability engineering can be employed including, but not limited to, liners, geo-membranes, compacted soils, imported sand, gravel or rock and gravity drainage contours to move fluids and gases away from impervious layers to egress exits. Impoundment floor and wall construction, can, but need not comprise, a stepped up or stepped down slope or bench as the case of mining course may dictate following the optimal ore grade mining. In any such stepped up or down applications, floor leveling and containment wall construction can typically drain or slope to one side or to a specific central gathering area(s) for removal of fluids by gravity drainage assistance.\|[0045] Optionally, capsule wall and floor construction can include insulation which prevents heat transfer outside of the constructed infrastructure or outside of inner capsules or conduits within the primary constructed capsule containment. Insulation can comprise manufactured materials, cement or various materials other materials which are less thermally conductive than surrounding masses, i.e. permeable body, formation, adjacent infrastructures, etc. Thermally insulating barriers can also be formed within the permeable body, along impoundment walls, ceilings, and/or floors. One detailed aspect includes the use of biodegradable insulating materials, e.g. soy insulation and the like. This is consistent with embodiments wherein the impoundment is a single use system such that insulations, pipes, and/or other components can have a relatively low useful life, e.g. less than 1-2 years. This can reduce equipment costs as well as reduce long-term environmental impact.\|[0046] These structures and methods can be applied at almost any scale. Larger encapsulated volumes and increased numbers of impoundments can readily produce hydrocarbon products and performance comparable to or exceeding smaller constructed infrastructures. As an illustration, single impoundments can range in size from tens of meters across to tens of acres. Optimal impoundment sizes may vary depending on the hydrocarbonaceous material and operating parameters, however it is expected that suitable areas can range from about one-half to five acres in top plan surface area.\|[0047] The methods and infrastructures can be used for recovery of hydrocarbons from a variety of hydrocarbonaceous materials. One particular advantage is a wide degree of latitude in controlling particle size, conditions, and composition of the permeable body introduced into the encapsulated volume. Non-limiting examples of mined hydrocarbonaceous material which can be treated comprise oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof. In some cases it can be desirable to provide a single type of hydro carbonaceous material so that the permeable body consists essentially of one of the above materials. However, the permeable body can include mixtures of these materials such that grade, oil content, hydrogen content, permeability and the like can be adjusted to achieve a desired result. Further, different hydrocarbon materials can be placed in multiple layers or in a mixed fashion such as combining coal, oil shale, tar sands, biomass, and/or peat.\|[0048] In one embodiment, hydrocarbon containing material can be classified into various inner capsules within a primary constructed infrastructure for optimization reasons. For instance, layers and depths of mined oil shale formations may be richer in certain depth pay zones as they are mined. Once blasted, mined, shoveled, and hauled inside of capsule for placement, richer oil bearing ores can be classified or mixed by richness for optimal yields, faster recovery, or for optimal averaging within each impoundment. Further, providing layers of differing composition can have added benefits. For example, a lower layer of tar sands can be oriented below an upper layer of oil shale. Generally, the upper and lower layers can be in direct contact with one another although this is not required. The upper layer can include heating pipes embedded therein as described in more detail below. The heating pipes can heat the oil shale sufficient to liberate kerogen oil, including short-chain liquid hydrocarbons, which can act as a solvent for bitumen removal from the tar sands. In this manner, the upper layer acts as an in situ solvent source for enhancing bitumen removal from the lower layer. Heating pipes within the lower layer are optional such that the lower layer can be free of heating pipes or may include heating pipes, depending on the amount of heat transferred via downward passing liquids from the upper layer and any other heat sources. The ability to selectively control the characteristics and composition of the permeable body adds a significant amount of freedom in optimizing oil yields and quality.\|[0049] Furthermore, in many embodiments, the liberated gaseous and liquid products act as an in situ produced solvent which supplements kerogen removal and/or additional hydrocarbon removal from the hydrocarbonaceous material.\|[0050] In yet another detailed aspect, the permeable body can further comprise an additive or biomass. Additives can include any composition which acts to increase the quality of removed hydrocarbons, e.g. increased API, decreased viscosity, improved flow properties, reduced wetting of residual shale, reduction of sulfur, hydrogenation agents, etc. Non-limiting examples of suitable additives can include bitumen, kerogen, propane, natural gas, natural gas condensate, crude oil, refining bottoms, asphaltenes, common solvents, other diluents, and combinations of these materials. In one specific embodiment, the additive can include a flow improvement agent and/or a hydrogen donor agent. Some materials can act as both or either agents to improve flow or as a hydrogen donor. Non-limiting examples of such additives can include methane, natural gas condensates, common solvent such as acetone, toluene, benzene, etc., and other additives listed above. Additives can act to increase the hydrogen to carbon ratio in any hydrocarbon products, as well as act as a flow enhancement agent. For example, various solvents and other additives can create a physical mixture which has a reduced viscosity and/or reduced affinity for particulate solids, rock, and the like. Further, some additives can chemically react with hydrocarbons and/or allow liquid flow of the hydrocarbon products. Any additives used can become part of a final recovered product or can be removed and reused or otherwise disposed of.\|[0051] Similarly, biological hydroxylation of hydrocarbonaceous materials to form synthetic gas or other lighter weight products can be accomplished using known additives and approaches. Enzymes or biocatalysts can also be used in a similar manner. Further, manmade materials can also be used as additives such as, but not limited to, tires, polymeric refuse, or other hydrocarbon-containing materials.\|[0052] Although these methods are broadly applicable, as a general guideline, the permeable body can include particles from about ⅛ inch to about 6 feet in largest dimension, and in some cases less than 1 foot and in other cases less than about 6 inches. However, as a practical matter, sizes from about 2 inches to about 2 feet can provide good results with about 1 foot diameter being useful for oil shale especially. Void space can be an important factor in determining optimal particle diameters. As a general matter, any functional void space can be used; however, about 10% to about 50% and in some cases about 30% to about 45% usually provides a good balance of permeability and effective use of available volumes. Void volumes can be varied somewhat by varying other parameters such as heating conduit placement, additives, and the like. Mechanical separation of mined hydrocarbonaceous materials allows creation of fine mesh, high permeability particles which enhance thermal dispersion rates once placed in capsule within the impoundment. The added permeability allows for more reasonable, low temperatures which also help to avoid higher temperatures which result in greater CO2 production from carbonate decomposition and associated release of trace heavy metals, volatile organics, and other compounds which can create toxic effluent and/or undesirable materials which are monitored and controlled.\|[0053] Carbon dioxide that is produced during the recovery process can be sequestered using one or more approaches. In particular, carbon dioxide can be converted to a solid or liquid form such that the associated carbon is precipitated or otherwise converted to a useful product. Such sequestering can be optionally accomplished by reacting carbon dioxide with an aqueous solution to form a precipitation of carbon dioxide with a metal. When referring to carbon dioxide precipitates or precipitating carbon dioxide, it is understood that precipitation consumes the carbon dioxide such that the carbon dioxide no longer exists as a CO2 structure. As such, the process is generally irreversible and differs from general adsorption techniques, which can also be used for sequestering carbon dioxide as further described herein. In one embodiment, the aqueous solution can be an ionic solution. In another embodiment, the aqueous solution can be salt water. The metal can be any metal that is capable of forming a solid with carbon dioxide including oxides thereof. In one embodiment, the metal can be calcium, magnesium, including oxides thereof, silicates thereof, and mixtures thereof. In one embodiment, the metal can be in the form of forsterite, serpentine and/or peridotite. In one embodiment, the exhausted hydrocarbonaceous materials can be injected or admixed with the carbon dioxide and salt water to form carbon dioxide precipitates. Such a process can take advantage of metals found in the exhausted hydrocarbonaceous materials.\|[0054] Additionally, other materials can be added to increase the reaction kinetics to form the carbon dioxide precipitate. For example, the addition of acids, catalysts, or other organic compounds may increase the reaction kinetics. Such sequestering can also produce heat during the sequestering process. In one embodiment, the heat can be redirected and applied to the heating step as discussed herein. Such recycling of heat can further provide a more efficient recovery system.\|[0055] Additionally, or alternatively, sequestering of carbon dioxide can be achieved by cryogenic precipitation forming liquid carbon dioxide. The collected carbon dioxide can be liquefied by lowering the temperature. Such liquid carbon dioxide can then be transferred to a container for disposal or for reuse. In one embodiment, the liquid carbon dioxide can be reacted to form polycarbonates, which can provide a stable form for disposal or potential use in other industries. In another embodiment, the liquid carbon dioxide can be used to further process the exhausted hydrocarbonaceous materials, as further discussed herein, including rinsing the hydrocarbonaceous materials during the recovery process. Such treatment can provide additional recovery of hydrocarbons that have not been removed during the initial recovery process as described herein.\|[0056] The sequestered carbon dioxide can be used in other commercial processes. In one embodiment, carbon dioxide can be used to isolate polymers from fluids. For example, carbon dioxide can be used to isolate polycarbonates from a solvent, e.g. methylene chloride. In another embodiment, carbon dioxide can be pumped into depleted permeable bodies. In the case of permeable bodies having a high coal content, once the initial stores of methane or other products are recovered, CO2 can be pumped into the impoundment, where it is stored in the coal, which can then provide the benefit of releasing additional methane. Between three and thirteen molecules of CO2 can be absorbed for each molecule of methane, making coal an excellent storage location for CO2.\|[0057] In one embodiment, storage of carbon dioxide can be performed in deep saline aquifers or brine-saturated rock formations that occur deep underground or under the ocean. Specifically, wells deep underground consisting of porous rock, such as limestone or sandstone, saturated with saltwater can form an effective trap for injected CO2. Geologically, over time, some CO2 can react with rock minerals to form solid carbonates, further immobilizing the same.\|[0058] Additionally, a liquid carbon dioxide can be optionally mixed and/or adsorbed by the exhausted hydrocarbonaceous materials. Such materials can then be disposed in an appropriate manner. When referring to liquid carbon dioxide, the embodiments herein can also be used with supercritical carbon dioxide. As such, the discussion and embodiments presented herein referring to liquid carbon dioxide also can be applied with respect to supercritical carbon dioxide.\|[0059] In another embodiment, sequestering carbon dioxide can be achieved by injecting exhausted hydrocarbonaceous materials with the carbon dioxide. Such injection can provide adsorption of carbon dioxide. Additionally, such process can be performed with a catalyst or without a catalyst. Other metal and organic additives can be included as discussed herein. In one embodiment, such sequestering can include a metal selected from the group consisting of calcium, magnesium, including oxides thereof, silicates thereof, and mixtures thereof.\|[0060] With respect to carbon dioxide sequestering, a constructed permeability control infrastructure can comprise a permeability control impoundment defining a substantially encapsulated volume wherein the permeability control impoundment is substantially free of undisturbed geological formations, a comminuted hydrocarbonaceous material within the encapsulated volume forming a permeable body of hydrocarbonaceous material, and a carbon dioxide collection unit operatively connected to collect carbon dioxide from the control infrastructure. It is understood that the infrastructure can include any of the elements described herein including those elements that have been referred to in the context of a process. Additionally, the methods and processes described herein can include any elements described herein including those elements that have been referred to in the context of a composition or system.\|[0061] The carbon dioxide can be collected consistent with one or more of the above approaches using a corresponding carbon dioxide control unit. In one optional aspect, the carbon dioxide control unit can include a vessel for treatment and/or storage of the carbon dioxide. Additional storage tanks, pumps and/or vessels can also be used for transporting or storage of treatment chemicals and by-products. As described herein, the vessel can contain an aqueous solution, a metal, and carbon dioxide where the vessel is configured to react the carbon dioxide with the aqueous solution to form a precipitation of carbon dioxide with the metal. In another embodiment, the vessel can contain carbon dioxide where the vessel is configured to form liquid carbon dioxide from the carbon dioxide by cryogenic precipitation. Additionally, the vessel can contain exhausted hydrocarbonaceous materials that adsorb the liquid carbon dioxide. In one embodiment, the vessel can contain carbon dioxide where the vessel is configured to mix exhausted hydrocarbonaceous materials with the carbon dioxide such that the exhausted hydrocarbonaceous materials adsorb the carbon dioxide.\|[0062] In one embodiment, computer assisted mining, mine planning, hauling, blasting, assay, loading, transport, placement, and dust control measures can be utilized to fill and optimize the speed of mined material movement into the constructed capsule containment structure. In one alternative aspect, the impoundments can be formed in excavated volumes of a hydrocarbonaceous formation, although other locations remote from the control infrastructure can also be useful. For example, some hydrocarbonaceous formations have relatively thin hydrocarbon-rich layers, e.g. less than about 300 feet thick. Therefore, vertical mining and drilling tend to not be cost effective. In such cases, horizontal mining can be useful to recover the hydrocarbonaceous materials for formation of the permeable body. Although horizontal mining continues to be a challenging endeavor, a number of technologies have been developed and continue to be developed which can be useful in connection with the impoundments. In such cases, at least a portion of the impoundment can be formed across a horizontal layer, while other portions of the impoundment can be formed along and/or adjacent non-hydrocarbon bearing formation layers. Other mining approaches such as, but not limited to, room and pillar mining can provide an effective source of hydrocarbonaceous material with minimal waste and/or reclamation which can be transported to an impoundment and treated in accordance with the these principles.\|[0063] As mentioned herein, these systems and processes allow for a large degree of control regarding properties and characteristics of the permeable body which can be designed and optimized for a given installation. Impoundments, individually and across a plurality of impoundments can be readily tailored and classified based on varying composition of materials, intended products and the like. For example, several impoundments can be dedicated to production of heavy crude oil, while others can be configured for production of lighter products and/or syn gas. Non-limiting example of potential classifications and factors can include catalyst activity, enzymatic reaction for specific products, aromatic compounds, hydrogen content, microorganism strain or purpose, upgrading process, target final product, pressure (effects product quality and type), temperature, swelling behavior, aquathermal reactions, hydrogen donor agents, heat superdisposition, garbage impoundment, sewage impoundment, reusable pipes, and others. Typically, a plurality of these factors can be used to configure impoundments in a given project area for distinct products and purposes.\|[0064] The comminuted hydrocarbonaceous material can be filled into the control infrastructure to form the permeable body in any suitable manner. Typically the comminuted hydrocarbonaceous material can be conveyed into the control infrastructure by dumping, conveyors or other suitable approaches. As mentioned previously, the permeable body can have a suitably high void volume. Indiscriminate dumping can result in excessive compaction and reduction of void volumes. Thus, the permeable body can be formed by low compaction conveying of the hydrocarbonaceous material into the infrastructure. For example, retracting conveyors can be used to deliver the material near a top surface of the permeable body as it is formed. In this way, the hydrocarbonaceous material can retain a significant void volume between particles without substantial further crushing or compaction despite some small degree of compaction which often results from lithostatic pressure as the permeable body is formed.\|[0065] Once a desired permeable body has been formed within the control infrastructure, heat can be introduced sufficient to begin removal of hydrocarbons, e.g. via pyrolysis. A suitable heat source can be thermally associated with the permeable body. Optimal operating temperatures within the permeable body can vary depending on the composition and desired products. However, as a general guideline, operating temperatures can range from about 200° F. to about 750° F. Temperature variations throughout the encapsulated volume can vary and may reach as high as 900° F. or more in some areas. In one embodiment, the operating temperature can be a relatively lower temperature to facilitate production of liquid product such as from about 200° F. to about 650° F. This heating step can be a roasting operation which results in beneficiation of the crushed ore of the permeable body. Further, one embodiment comprises controlling the temperature, pressure and other variables sufficient to produce predominantly, and in some cases substantially only, liquid product. Generally, products can include both liquid and gaseous products, while liquid products can require fewer processing steps such as scrubbers etc. The relatively high permeability of the permeable body allows for production of liquid hydrocarbon products and minimization of gaseous products, depending to some extent on the particular starting materials and operating conditions. In one embodiment, the recovery of hydrocarbon products can occur substantially in the absence of cracking within the permeable body.\|[0066] In one aspect, heat can be transferred to the permeable body via convection. Heated gases can be injected into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body. Heated gases can be produced by combustion of natural gas, hydrocarbon product, or any other suitable source. Non-limiting examples of suitable heat transfer fluids can include hot air, hot exhaust gases, steam, hydrocarbon vapors and/or hot liquids. The heated gases can be imported from external sources or recovered from the process.\|[0067] Alternatively, or in combination with convective heating, a highly configurable approach can include embedding a plurality of conduits within the permeable body. The conduits can be configured for use as heating pipes, cooling pipes, heat transfer pipes, drainage pipes, or gas pipes. Further, the conduits can be dedicated to a single function or may serve multiple functions during operation of the infrastructure, i.e. heat transfer and drainage. The conduits can be formed of any suitable material, depending on the intended function. Non-limiting examples of suitable materials can include clay pipes, refractory cement pipes, refractory ECC pipes, poured in place pipes, metal pipes such as cast iron, stainless steel etc., polymer such as PVC, and the like. In one specific embodiment, all or at least a portion of the embedded conduits can comprise a degradable material. For example, non-galvanized 6″ cast iron pipes can be effectively used for single use embodiments and perform well over the useful life of the impoundment, typically less than about 2 years. Further, different portions of the plurality of conduits can be formed of different materials. Poured in place pipes can be especially useful for very large encapsulation volumes where pipe diameters exceed several feet. Such pipes can be formed using flexible wraps which retain a viscous fluid in an annular shape. For example, PVC pipes can be used as a portion of a form along with flexible wraps, where concrete or other viscous fluid is pumped into an annular space between the PVC and flexible wrap. Depending on the intended function, perforations or other apertures can be made in the conduits to allow fluids to flow between the conduits and the permeable body. Typical operating temperatures exceed the melting point of conventional polymer and resin pipes. In some embodiments, the conduits can be placed and oriented such that the conduits intentionally melt or otherwise degrade during operation of the infrastructure.\|[0068] The plurality of conduits can be readily oriented in any configuration, whether substantially horizontal, vertical, slanted, branched, or the like. At least a portion of the conduits can be oriented along predetermined pathways prior to embedding the conduits within the permeable body. The predetermined pathways can be designed to improve heat transfer, gas-liquid-solid contacting, maximize fluid delivery or removal from specific regions within the encapsulated volume, or the like. Further, at least a portion the conduits can be dedicated to heating of the permeable body. These heating conduits can be selectively perforated to allow heated gases or other fluids to convectively heat and mix throughout the permeable body. The perforations can be located and sized to optimize even and/or controlled heating throughout the permeable body. Alternatively, the heating conduits can form a closed loop such that heating gases or fluids are segregated from the permeable body. Thus, a “closed loop” does not necessarily require recirculation, rather isolation of heating fluid from the permeable body. In this manner, heating can be accomplished primarily or substantially only through thermal conduction across the conduit walls from the heating fluids into the permeable body. Heating in a closed loop allows for prevention of mass transfer between the heating fluid and permeable body and can reduce formation and/or extraction of gaseous hydrocarbon products.\|[0069] During the heating or roasting of the permeable body, localized areas of heat which exceed parent rock decomposition temperatures, often above about 900° F., can reduce yields and form carbon dioxide and undesirable contaminating compounds which can lead to leachates containing heavy metals, soluble organics and the like. The heating conduits can allow for substantial elimination of such localized hot spots while maintaining a vast majority of the permeable body within a desired temperature range. The degree of uniformity in temperature can be a balance of cost (e.g. for additional heating conduits) versus yields. However, at least about 85% of the permeable body can readily be maintained within about 5-10% of a target temperature range with substantially no hot spots, i.e. exceeding the decomposition temperature of the hydrocarbonaceous materials such as about 800° F. and in many cases about 900° F. Thus, operated as described herein, the systems can allow for recovery of hydrocarbons while eliminating or substantially avoiding production of undesirable leachates. Although products can vary considerably depending on the starting materials, high quality liquid and gaseous products are possible. In accordance with one embodiment, a crushed oil shale material can produce a liquid product having an API from about 30 to about 45, with about 33 to about 38 being currently typical, directly from the oil shale without additional treatment. Interestingly, practice of these processes has led to an understanding that pressure appears to be a much less influential factor on the quality of recovered hydrocarbons than temperature and heating times. Although heating times can vary considerably, depending on void space, permeable body composition, quality, etc., as a general guideline times can range from a few days (i.e. 3-4 days) up to about one year. In one specific example, heating times can range from about 2 weeks to about 4 months. Under-heating oil shale at short residence times, i.e. minutes to several hours, can lead to formation of leachable and/or somewhat volatile hydrocarbons. Accordingly, these systems and methods allow for extended residence times at moderate temperatures such that organics present in oil shale can be volatilized and/or carbonized, leaving insubstantial leachable organics. In addition, the underlying shale is not generally decomposed or altered which reduces soluble salt formation.\|[0070] Further, conduits can be oriented among a plurality of impoundments and/or control infrastructures to transfer fluids and/or heat between the structures. The conduits can be welded to one another using conventional welding or the like. Further, the conduits can include junctions which allow for rotation and or small amounts of movement during expansion and subsidence of material in the permeable body. Additionally, the conduits can include a support system which acts to support the assembly of conduits prior to and during filling of the encapsulated volume, as well as during operation. For example, during heating flows of fluids, heating and the like can cause expansion (fracturing or popcorn effect) or subsidence sufficient to create potentially damaging stress and strain on the conduits and associated junctions. A truss support system or other similar anchoring members can be useful in reducing damage to the conduits. The anchoring members can include cement blocks, 1-beams, rebar, columns, etc. which can be associated with walls of the impoundment, including side walls, floors and ceilings.\|[0071] Alternatively, the conduits can be completely constructed and assembled prior to introduction of any mined materials into the encapsulated volume. Care and planning can be considered in designing the predetermined pathways of the conduits and method of filling the volume in order to prevent damage to the conduits during the filling process as the conduits are buried. Thus, as a general rule, the conduits are oriented ab initio, or prior to embedding in the permeable body such that they are non-drilled. As a result, construction of the conduits and placement thereof can be performed without extensive core drilling and/or complicated machinery associated with well-bore or horizontal drilling. Rather, horizontal or any other orientation of conduit can be readily achieved by assembling the desired predetermined pathways prior to, or contemporaneous with, filling the infrastructure with the mined hydrocarbonaceous material. The non-drilled, hand/crane-placed conduits oriented in various geometric patterns can be laid with valve controlled connecting points which yield precise and closely monitored heating within the capsule impoundment. The ability to place and layer conduits including connecting, bypass and flow valves, and direct injection and exit points, allow for precision temperature and heating rates, precision pressure and pressurization rates, and precision fluid and gas ingress, egress and composition admixtures. For example, when a bacteria, enzyme, or other biological material is used, optimal temperatures can be readily maintained throughout the permeable body to increase performance, reaction, and reliability of such biomaterials.\|[0072] The conduits will generally pass through walls of the constructed infrastructure at various points. Due to temperature differences and tolerances, it can be beneficial to include an insulating material at the interface between the wall and the conduits. The dimensions of this interface can be minimized while also allowing space for thermal expansion differences during startup, steady-state operation, fluctuating operating conditions, and shutdown of the infrastructure. The interface can also involve insulating materials and sealant devices which prevent uncontrolled egress of hydrocarbons or other materials from the control infrastructure. Non-limiting examples of suitable materials can include high temperature gaskets, metal alloys, ceramics, clay or mineral liners, composites or other materials which having melting points above typical operating temperatures and act as a continuation of the permeability control provided by walls of the control infrastructure.\|[0073] Further, walls of the constructed infrastructure can be configured to minimize heat loss. In one aspect, the walls can be constructed having a substantially uniform thickness which is optimized to provide sufficient mechanical strength while also minimizing the volume of wall material through which the conduits pass. Specifically, excessively thick walls can reduce the amount of heat which is transferred into the permeable body by absorbing the same through conduction. Conversely, the walls can also act as a thermal barrier to somewhat insulate the permeable body and retain heat therein during operation.\|[0074] In one embodiment, fluid and gas compounds within the permeable body can be altered for desired extractive products using, as an example, induced pressure through gases or piled lithostatic pressure from piled rubble. Thus, some degree of upgrading and/or modification can be accomplished simultaneous with the recovery process. Further, certain hydro carbonaceous materials can require treatment using specific diluents or other materials. For example, treatment of tar sands can be readily accomplished by steam injection or solvent injection to facilitate separation of bitumen from sand particles according to well known mechanisms.\|[0075] With the above description in mind, FIG. 1 depicts a side view of one embodiment showing an engineered capsule containment and extraction impoundment 100 where existing grade 108 is used primarily as support for the impermeable floor layer 112. Exterior capsule impoundment side walls 102 provide containment and can, but need not be, subdivided by interior walls 104. Subdividing can create separate containment capsules 122 within a greater capsule containment of the impoundment 100 which can be any geometry, size or subdivision. Further subdivisions can be horizontally or vertically stacked. By creating separate containment capsules 122 or chambers, classification of lower grade materials, varied gases, varied liquids, varied process stages, varied enzymes or microbiology types, or other desired and staged processes can be readily accommodated. Sectioned capsules constructed as silos within larger constructed capsules can also be designed to provide staged and sequenced processing, temperatures, gas and fluid compositions and thermal transfers. Such sectioned capsules can provide additional environmental monitoring and can be built of lined and engineered tailings berms similar to the primary exterior walls. In one embodiment, sections within the impoundment 100 can be used to place materials in isolation, in the absence of external heat, or with the intent of limited or controlled combustion or solvent application. Lower content hydrocarbon bearing material can be useful as a combustion material or as fill or a berm wall building material. Material which does not meet a various cut-off grade thresholds can also be sequestered without alteration in an impoundment dedicated for such purpose. In such embodiments, such areas may be completely isolated or bypassed by heat, solvents, gases, liquids, or the like. Optional monitoring devices and/or equipment can be permanently or temporarily installed within the impoundment or outside perimeters of the impoundments in order to verify containment of the sequestered material.\|[0076] Walls 102 and 104 as well as cap 116 and impermeable layer 112 can be engineered and reinforced by gabions 146 and or geogrid 148 layered in fill compaction. Alternatively, these walls 102, 104, 116 and 112 which comprise the permeability control impoundment and collectively define the encapsulated volume can be formed of any other suitable material as previously described. In this embodiment, the impoundment 100 includes side walls 102 and 104 which are self-supporting. In one embodiment, tailings berms, walls, and floors can be compacted and engineered for structure as well as permeability. The use of compacted geogrids and other deadman structures for support of berms and embankments can be included prior to or incorporated with permeability control layers which may include sand, clay, bentonite clay, gravel, cement, grout, reinforced cement, refractory cements, insulations, geo-membranes, drainpipes, temperature resistant insulations of penetrating heated pipes, etc.\|[0077] In one alternative embodiment, the permeability control impoundment can include side walls which are compacted earth and/or undisturbed geological formations while the cap and floors are impermeable. Specifically, in such embodiments an impermeable cap can be used to prevent uncontrolled escape of volatiles and gases from the impoundment such that appropriate gas collection outlets can be used. Similarly, an impermeable floor can be used to contain and direct collected liquids to a suitable outlet such the drain system 133 to remove liquid products from lower regions of the impoundment. Although impermeable side walls can be desirable in some embodiments, such are not always required. In some cases, side walls can be exposed undisturbed earth or compacted fill or earth, or other permeable material. Having permeable side walls may allow some small egress of gases and/or liquids from the impoundment.\|[0078] Although not shown, above, below, around and adjacent to constructed capsule containment vessels environmental hydrology measures can be engineered to redirect surface water away from the capsule walls, floors, caps, etc. during operation. Further, gravity assisted drainage pipes and mechanisms can be utilized to aggregate and channel fluids, liquids or solvents within the encapsulated volume to central gathering, pumping, condensing, heating, staging and discharge pipes, silos, tanks, and/or wells as needed. In a similar manner, steam and/or water which is intentionally introduce, e.g. for tar sands bitumen treatment, can be recycled.\|[0079] Once wall structures 102 and 104 have been constructed above a constructed and impermeable floor layer 112 which commences from ground surface 106, the mined rubble 120 (which may be crushed or classified according to size or hydrocarbon richness), can be placed in layers upon (or next to) placed tubular heating pipes 118, fluid drainage pipes 124, and, or gas gathering or injection pipes 126. These pipes can be oriented and designed in any optimal flow pattern, angle, length, size, volume, intersection, grid, wall sizing, alloy construction, perforation design, injection rate, and extraction rate. In some cases, pipes such as those used for heat transfer can be connected to, recycled through or derive heat from heat source 134. Alternatively, or in combination with, recovered gases can be condensed by a condenser 140. Heat recovered by the condenser can be optionally used to supplement heating of the permeable body or for other process needs.\|[0080] Heat source 134 can derive, amplify, gather, create, combine, separate, transmit or include heat derived from any suitable heat source including, but not limited to, fuel cells (e.g. solid oxide fuel cells, molten carbonate fuel cells and the like), solar sources, wind sources, hydrocarbon liquid or gas combustion heaters, geothermal heat sources, nuclear power plant, coal fired power plant, radio frequency generated heat, wave energy, flameless combustors, natural distributed combustors, or any combination thereof. In some cases, electrical resistive heaters or other heaters can be used, although fuel cells and combustion-based heaters are particularly effective. In some locations, geothermal water can be circulated to the surface in adequate amounts to heat the permeable body and directed into the infrastructure.\|[0081] In another embodiment, electrically conductive material can be distributed throughout the permeable body and an electric current can be passed through the conductive material sufficient to generate heat. The electrically conductive material can include, but is not limited to, metal pieces or beads, conductive cement, metal coated particles, metal-ceramic composites, conductive semi-metal carbides, calcined petroleum coke, laid wire, combinations of these materials, and the like. The electrically conductive material can be premixed having various mesh sizes or the materials can be introduced into the permeable body subsequent to formation of the permeable body.\|[0082] Liquids or gases can transfer heat from heat source 134, or in another embodiment, in the cases of hydrocarbon liquid or gas combustion, radio frequency generators (microwaves), or fuel cells all can, but need not, actually generate heat inside of capsule impoundment area 114 or 122. In one embodiment, heating of the permeable body can be accomplished by convective heating from hydrocarbon combustion. Of particular interest is hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen. Stoichiometric conditions can allow for significantly increased heat gas temperatures. Stoichiometric combustion can employ but does not generally require a pure oxygen source which can be provided by known technologies including, but not limited to, oxygen concentrators, membranes, electrolysis, and the like. In some embodiments oxygen can be provided from air with stoichiometric amounts of oxygen and hydrogen. Combustion off gas can be directed to an ultra-high temperature heat exchanger, e.g. a ceramic or other suitable material having an operating temperature above about 2500° F. Air obtained from ambient or recycled from other processes can be heated via the ultra high temperature heat exchanger and then sent to the impoundment for heating of the permeable body. The combustion off gases can then be sequestered without the need for further separation, i.e. because the off gas is predominantly carbon dioxide and water.\|[0083] In order to minimize heat losses, distances can be minimized between the combustion chamber, heat exchanger, and impoundments. Therefore, in one specific detailed embodiment portable combustors can be attached to individual heating conduits or smaller sections of conduits. Portable combustors or burners can individually provide from about 100,000 Btu to about 1,000,000 Btu with about 600,000 Btu per pipe generally being sufficient.\|[0084] Alternatively, in-capsule combustion can be initiated inside of isolated capsules within a primary constructed capsule containment structure. This process partially combusts hydrocarbonaceous material to provide heat and intrinsic pyrolysis. Unwanted air emissions 144 can be captured and sequestered in a formation 108 once derived from capsule containment 114, 122 or from heat source 134 and delivered by a drilled well bore 142. Heat source 134 can also create electricity and transmit, transform or power via electrical transmission lines 150. The liquids or gases extracted from capsule impoundment treatment area 114 or 122 can be stored in a nearby holding tank 136 or within a capsule containment 114 or 122. For example, the impermeable floor layer 112 can include a sloped area 110 which directs liquids towards drain system 133 where liquids are directed to the holding tank.\|[0085] As rubble material 120 is placed with piping 118, 124, 126, and 128, various measurement devices or sensors 130 are envisioned to monitor temperature, pressure, fluids, gases, compositions, heating rates, density, and all other process attributes during the extractive process within, around, or underneath the engineered capsule containment impoundment 100. Such monitoring devices and sensors 130 can be distributed anywhere within, around, part of, connected to, or on top of placed piping 118, 124, 126, and 128 or, on top of, covered by, or buried within rubble material 120 or impermeable barrier zone 112.\|[0086] As placed rubble material 120 fills the capsule treatment area 114 or 122, 120 becomes the ceiling support for engineered impermeable cap barrier zone 138, and wall barrier construction 170, which may include any combination of impermeability and engineered fluid and gas barrier or constructed capsule construction comprising those which may make up 112 including, but not limited to clay 162, compacted fill or import material 164, cement or refractory cement containing material 166, geo synthetic membrane, liner or insulation 168. Above 138, fill material which can be oriented as ceiling cap 116 is placed to create lithostatic pressure upon the capsule treatment areas 114 or 122. Covering the permeable body with compacted fill sufficient to create an increased lithostatic pressure within the permeable body can be useful in further increasing hydrocarbon product quality. A compacted fill ceiling can substantially cover the permeable body, while the permeable body in return can substantially support the compacted fill ceiling. The compacted fill ceiling can further be sufficiently impermeable to removed hydrocarbon or an additional layer of permeability control material can be added in a similar manner as side and/or floor walls. Additional pressure can be introduced into extraction capsule treatment area 114 or 122 by increasing any gas or fluid once extracted, treated or recycled, as the case may be, via any of piping 118, 124, 126, or 128. All relative measurements, optimization rates, injection rates, extraction rates, temperatures, heating rates, flow rates, pressure rates, capacity indicators, chemical compositions, or other data relative to the process of heating, extraction, stabilization, sequestration, impoundment, upgrading, refining or structure analysis within the capsule impoundment 100 are envisioned through connection to a computing device 132 which operates computer software for the management, calculation and optimization of the entire process. Further, core drilling, geological reserve analysis and assay modeling of a formation prior to blasting, mining and hauling (or at any time before, after or during such tasks) can serve as data input feeds into computer controlled mechanisms that operate software to identify optimal placements, dimensions, volumes and designs calibrated and cross referenced to desired production rate, pressure, temperature, heat input rates, gas weight percentages, gas injection compositions, heat capacity, permeability, porosity, chemical and mineral composition, compaction, density. Such analysis and determinations may include other factors like weather data factors such as temperature and air moisture content impacting the overall performance of the constructed infrastructure. Other data such as ore moisture content, hydrocarbon richness, weight, mesh size, and mineral and geological composition can be utilized as inputs including time value of money data sets yielding project cash flows, debt service, and internal rates of return.\|[0087] FIG. 2A shows a collection of impoundments including an uncovered or uncapped capsule impoundment 100, containing sectioned capsule impoundments 122 inside of a mining quarry 200 with various elevations of bench mining. FIG. 2B illustrates a single impoundment 122 without associated conduits and other aspects merely for clarity. This impoundment can be similar to that illustrated in FIG. 1 or any other configuration. In some embodiments, it is envisioned that mining rubble can be transferred down chutes 230 or via conveyors 232 to the quarry capsule impoundments 100 and 122 without any need of mining haul trucks.\|[0088] FIG. 3 shows the engineered permeability barriers 112 below capsule impoundment 100 resting on existing grade 106 of formation 108 with cap covering material or fill 302 on the sides and top of capsule impoundment 100 to ultimately (following the process) cover and reclaim a new earth surface 300. Indigenous plants which may have been temporarily moved from the area may be replanted such as trees 306. The constructed infrastructures can generally be single use structures which can be readily and securely shut down with minimal additional remediation. This can dramatically reduce costs associated with moving large volumes of spent materials. However, in some circumstances the constructed infrastructures can be excavated and reused. Some equipment such as radio frequency (RF) mechanisms, tubulars, devices, and emitters may be recovered from within the constructed impoundment upon completion of hydrocarbon recovery.\|[0089] FIG. 4 shows computer means 130 controlling various property inputs and outputs of conduits 118, 126, or 128 connected to heat source 134 during the process among the subdivided impoundments 122 within a collective impoundment 100 to control heating of the permeable body. Similarly, liquid and vapor collected from the impoundments can be monitored and collected in tank 136 and condenser 140, respectively. Condensed liquids from the condenser can be collected in tank 141, while non-condensable vapor collected at unit 143. As described previously, the liquid and vapor products can be combined or more often left as separate products depending on condensability, target product, and the like. A portion of the vapor product can be optionally condensed and combined with the liquid products in tank 136. However, much of the vapor product will be C4 and lighter gases which can be burned, sold, or used within the process. For example, hydrogen gas may be recovered using conventional gas separation and used to hydrotreat the liquid products according to conventional upgrading methods, e.g. catalytic, etc. or the non-condensable gaseous product can be burned to produce heat for use in heating the permeable body, heating an adjacent or nearby impoundment, heating service or personnel areas, or satisfying other process heat requirements. The constructed infrastructure can include thermocouples, pressure meters, flow meters, fluid dispersion sensors, richness sensors and any other conventional process control devices distributed throughout the constructed infrastructure. These devices can be each operatively associated with a computer such that heating rates, product flow rates, and pressures can be monitored or altered during heating of the permeable body. Optionally, in-place agitation can be performed using, for example, ultrasonic generators which are associated with the permeable body. Such agitation can facilitate separation and pyrolysis of hydrocarbons from the underlying solid materials with which they are associated. Further, sufficient agitation can reduce clogging and agglomeration throughout the permeable body and the conduits.\|[0090] FIG. 5 shows how any of the conduits can be used to transfer heat in any form of gas, liquid or heat via transfer means 510 from any sectioned capsule impoundment to another. Then, cooled fluid can be conveyed via heat transfer means 512 to the heat originating capsule 500, or heat originating source 134 to pick up more heat from capsule 500 to be again recirculated to a destination capsule 522. Thus, various conduits can be used to transfer heat from one impoundment to another in order to recycle heat and manage energy usage to minimize energy losses.\|[0091] In yet another aspect, a hydrogen donor agent can be introduced into the permeable body during the step of heating. The hydrogen donor agent can be any composition which is capable of hydrogenation of the hydrocarbons and can optionally be a reducing agent. Non-limiting examples of suitable hydrogen donor agents can include synthesis gas, propane, methane, hydrogen, natural gas, natural gas condensate, industrial solvents such as acetones, toluenes, benzenes, xylenes, cumenes, cyclopentanes, cyclohexanes, lower alkenes (C4-C10), terpenes, substituted compounds of these solvents, etc., and the like. Further, the recovered hydrocarbons can be subjected to hydrotreating either within the permeable body or subsequent to collection. Advantageously, hydrogen recovered from the gas products can be reintroduced into the liquid product for upgrading. Regardless, hydrotreating or hydrodesulfurization can be very useful in reducing nitrogen and sulfur content in final hydrocarbon products. Optionally, catalysts can be introduced to facilitate such reactions. In addition, introduction of light hydrocarbons into the permeable body can result in reforming reactions which reduce the molecular weight, while increasing the hydrogen to carbon ratio. This is particularly advantageous due at least in part to high permeability of the permeable body, e.g. often around 30%-40% void volume although void volume can generally vary from about 10% to about 50% void volume. Light hydrocarbons which can be injected can be any which provide reforming to recovered hydrocarbons. Non-limiting examples of suitable light hydrocarbons include natural gas, natural gas condensates, industrial solvents, hydrogen donor agents, and other hydrocarbons having ten or fewer carbons, and often five or fewer carbons. Currently, natural gas is an effective, convenient, and plentiful light hydrocarbon. As mentioned previously, various solvents or other additives can also be added to aid in extraction of hydrocarbon products from the oil shale and can often also increase fluidity.\|[0092] The light hydrocarbon can be introduced into the permeable body by conveying the same through a delivery conduit having an open end in fluid communication with a lower portion of the permeable body such that the light hydrocarbons (which are a gas under normal operating conditions) permeate up through the permeable body. Alternatively, this same approach can be applied to recovered hydrocarbons which are first delivered to an empty impoundment. In this way, the impoundment can act as a holding tank for direct products from a nearby impoundment and as a reformer or upgrader. In this embodiment, the impoundment can be at least partially filled with a liquid product where the gaseous light hydrocarbon is passed through and allowed to contact the liquid hydrocarbon products at temperatures and conditions sufficient to achieve reforming in accordance with well known processes. Optional reforming catalysts which include metals such as Pd, Ni or other suitable catalytically active metals can also be included in the liquid product within the impoundment. The addition of catalysts can serve to lower and/or adjust reforming temperature and/or pressure for particular liquid products. Further, the impoundments can be readily formed at almost any depth. Thus, optimal reforming pressures (or recovery pressures when using impoundment depth as pressure control measure for recovery from a permeable body) can be designed based on hydrostatic pressure due to the amount of liquid in the impoundment and the height of the impoundment, i.e. P=ρgh. In addition, the pressure can vary considerably over the height of the impoundment sufficient to provide multiple reforming zones and tailorable pressures. Generally, pressures within the permeable body can be sufficient to achieve substantially only liquid extraction, although some minor volumes of vapor may be produced depending on the particular composition of the permeable body. As a general guideline, pressures can range from about 5 atm to about 50 atm, although pressures from about 6 atm to about 20 atm can be particularly useful. However, any pressure greater than about atmospheric can be used.\|[0093] In one embodiment, extracted crude has fines precipitated out within the subdivided capsules. Extracted fluids and gases can be treated for the removal of fines and dust particles. Separation of fines from shale oil can be accomplished by techniques such as, but not limited to, hot gas filtering, precipitation, and heavy oil recycling.\|[0094] Hydrocarbon products recovered from the permeable body can be further processed (e.g. refined) or used as produced. Any condensable gaseous products can be condensed by cooling and collection, while non-condensable gases can be collected, burned as fuel, reinjected, or otherwise utilized or disposed of. Optionally, mobile equipment can be used to collect gases. These units can be readily oriented proximate to the control infrastructure and the gaseous product directed thereto via suitable conduits from an upper region of the control infrastructure.\|[0095] In yet another alternative embodiment, heat within the permeable body can be recovered subsequent to primary recovery of hydrocarbon materials therefrom. For example, a large amount of heat is retained in the permeable body. In one optional embodiment, the permeable body can be flooded with a heat transfer fluid such as water to form a heated fluid, e.g. heated water and/or steam. At the same time, this process can facilitate removal of some residual hydrocarbon products via a physical rinsing of the spent shale solids. In some cases, the introduction of water and presence of steam can result in water gas shift reactions and formation of synthesis gas. Steam recovered from this process can be used to drive a generator, directed to another nearby infrastructure, or otherwise used. Hydrocarbons and/or synthesis gas can be separated from the steam or heated fluid by conventional methods.\|[0096] Although the methods and infrastructure allow for improved permeability and control of operating conditions, significant quantities of unrecovered hydrocarbons, precious metals, minerals, sodium bicarbonate or other commercially valuable materials often remain in the permeable body. Therefore, a selective solvent can be injected or introduced into the permeable body. Typically, this can be done subsequent to collecting the hydrocarbons, although certain selective solvents can be beneficially used prior to heating and/or collection. This can be done using one or more of the existing conduits or by direct injection and percolation through the permeable body. The selective solvent or leachate can be chosen as a solvent for one or more target materials, e.g. minerals, precious metal, heavy metals, hydrocarbons, or sodium bicarbonate. In one specific embodiment, steam or carbon dioxide can be used as a rinse of the permeable body to dislodge at least a portion of any remaining hydrocarbons. This can be beneficial not only in removing potentially valuable secondary products, but also in cleaning remaining spent materials of trace heavy metal or inorganics to below detectable levels in order to comply with regulatory standards or to prevent inadvertent leaching of materials at a future date.\|[0097] More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body. Typically, such recovery of materials can be performed prior to heat treatment of the permeable body. Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like. For example, heavy metals, bauxite or aluminum, and mercury can be removed by flooding the permeable body with an appropriate solvent and recirculating the resulting leachate through appropriately designed ion exchange resins (e.g. beads, membranes, etc.).\|[0098] Similarly, bioextraction, bioleaching, biorecovery, or bioremediation of hydrocarbon material, spent materials, or precious metals can be performed to further improve remediation, extract valuable metals, and restoration of spent material to environmentally acceptable standards. In such bioextraction scenarios, conduits can be used to inject catalyzing gases as a precursor which helps to encourage bioreaction and growth. Such microorganisms and enzymes can biochemically oxidize the ore body or material or cellulosic or other biomass material prior to an ore solvent extraction via bio-oxidation. For example, a perforated pipe or other mechanism can be used to inject a light hydrocarbon (e.g. methane, ethane, propane or butane) into the permeable body sufficient to stimulate growth and action of native bacteria. Bacteria can be native or introduced and may grow under aerobic or anaerobic conditions. Such bacteria can release metals from the permeable body which can then be recovered via flushing with a suitable solvent or other suitable recovery methods. The recovered metals can then be precipitated out using conventional methods.\|[0099] Synthesis gas can also be recovered from the permeable body during the step of heating. Various stages of gas production can be manipulated through processes which raise or lower operating temperatures within the encapsulated volume and adjust other inputs into the impoundment to produce synthetic gases which can include but are not limited to, carbon monoxide, hydrogen, hydrogen sulfide, hydrocarbons, ammonia, water, nitrogen or various combinations thereof. In one embodiment, temperature and pressure can be controlled within the permeable body to lower CO2 emissions as synthetic gases are extracted.\|[0100] Hydrocarbon product recovered from the constructed infrastructures can most often be further processed, e.g. by upgrading, refining, etc. Sulfur from related upgrading and refining processing can be isolated in various constructed sulfur capsules within the greater structured impoundment capsule. Constructed sulfur capsules can be spent constructed infrastructures or dedicated for the purpose of storage and isolation after desulfurization.\|[0101] Similarly, spent hydrocarbonaceous material remaining in the constructed infrastructure can be utilized in the production of cement and aggregate products for use in construction or stabilization of the infrastructure itself or in the formation of offsite constructed infrastructures. Such cement products made with the spent shale may include, but are not limited to, mixtures with Portland cement, calcium salt, volcanic ash, perlite, synthetic nano carbons, sand, fiber glass, crushed glass, asphalt, tar, binding resins, cellulosic plant fibers, and the like.\|[0102] In still another embodiment, injection, monitoring and production conduits or extraction egresses can be incorporated into any pattern or placement within the constructed infrastructure. Monitoring wells and constructed geo membrane layers beneath or outside of the constructed capsule containment can be employed to monitor unwanted fluid and moisture migration outside of containment boundaries and the constructed infrastructure.\|[0103] Although a filled and prepared constructed infrastructure can often be immediately heated to recover hydrocarbons, this is not required. For example, a constructed infrastructure which is built and filled with mined hydrocarbonaceous material can be left in place as a proven reserve. Such structures are less susceptible to explosion or damage due to terrorist activity and can also provide strategic reserves of unprocessed petroleum products, with classified and known properties so that economic valuations can be increased and more predictable. Long term petroleum storage often faces quality deterioration issues over time. Thus, these approaches can optionally be used for long term quality insurance and storage with reduced concerns regarding breakdown and degradation of hydrocarbon products.\|[0104] In still another aspect, the high quality liquid product can be blended with more viscous lower quality (e.g. lower API) hydrocarbon products. For example, kerogen oil produced from the impoundments can be blended with bitumen to form a blended oil. The bitumen is typically not transportable through an extended pipeline under conventional and accepted pipeline standards and can have a viscosity substantially above and an API substantially below that of the kerogen oil. By blending the kerogen oil and bitumen, the blended oil can be rendered transportable without the use of additional diluents or other viscosity or API modifiers. As a result, the blended oil can be pumped through a pipeline without requiring additional treatments to remove a diluent or returning such diluents via a secondary pipeline. Conventionally, bitumen is combined with a diluent such as natural gas condensate or other low molecular weight liquids, to allow pumping to a remote location. The diluent is removed and returned via a second pipeline back to the bitumen source. These approaches allow for elimination of returning diluent and simultaneous upgrading of the bitumen.\|[0105] Difficult problems can thus be solved related to the extraction of hydrocarbon liquids and gases from surface or underground mined hydrocarbon bearing deposits such as oil shale, tar sands, lignite, and coal, and from harvested biomass. Among other things, these methods and systems help reduce cost, increase volume output, lower air emissions, limit water consumption, prevent underground aquifer contamination, reclaim surface disturbances, reduce material handling costs, remove dirty fine particulates, and improve composition of recovered hydrocarbon liquid or gas. Water contamination issues can also be addressed with a safer, more predictable, engineered, observable, repairable, adaptable and preventable water protection structure.\|[0106] Although the described methods and systems are mining-dependent, they are not limited or encumbered to conventional aboveground (ex-situ) retorting processes. This approach improves upon the benefits of surface retorts including better process control of temperature, pressure, injection rates, fluid and gas compositions, product quality and better permeability due to processing and heating mined rubble. These advantages are available while still addressing the volume, handling, and scalability issues most fabricated surface retorts cannot provide.\|[0107] Other improvements which can be realized are related to environmental protection. Conventional surface retorts have had the problem of spent shale after it has been mined and has passed through a surface retort. Spent shale which has been thermally altered requires special handling to reclaim and isolate from surface drainage basins and underground aquifers. These methods and systems can address reclamation and retorting in a uniquely combined approach. In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants.\|[0108] It is to be understood that the above-referenced arrangements are illustrative of the application for the principles of the present invention. Thus, while the present invention has been described above in connection with the exemplary embodiments, it will be apparent to those of ordinary skill in the art that numerous modifications and alternative arrangements can be made without departing from the principles and concepts of the invention as set forth in the claims.	(US8323481)\|RELATED APPLICATION\|[0001] This application claims priority to U.S. Provisional Patent Application No. 61/152,220 filed Feb. 12, 2009 which is incorporated herein by reference.\|(US8323481)\|BACKGROUND\|[0002] Global and domestic demand for fossil fuels continues to rise despite price increases and other economic and geopolitical concerns. As such demand continues to rise, research and investigation into finding additional economically viable sources of fossil fuels correspondingly increases. Historically, many have recognized the vast quantities of energy stored in oil shale, coal and tar sand deposits, for example. However, these sources remain a difficult challenge in terms of economically competitive recovery. Canadian tar sands have shown that such efforts can be fruitful, although many challenges still remain, including environmental impact, product quality, production costs and process time, among others.\|[0003] Estimates of world-wide oil shale reserves range from two to almost seven trillion barrels of oil, depending on the estimating source. Regardless, these reserves represent a tremendous volume and remain a substantially untapped resource. A large number of companies and investigators continue to study and test methods of recovering oil from such reserves. In the oil shale industry, methods of extraction have included underground rubble chimneys created by explosions, in-situ methods such as In-Situ Conversion Process (ICP) method (Shell Oil), and heating within steel fabricated retorts. Other methods have included in-situ radio frequency methods (microwaves), and “modified” in-situ processes wherein underground mining, blasting and retorting have been combined to make rubble out of a formation to allow for better heat transfer and product removal.\|[0004] Among typical oil shale processes, all face tradeoffs in economics and environmental concerns. No current process alone satisfies economic, environmental, and technical challenges. Moreover, global warming concerns give rise to additional measures to address carbon dioxide (CO2) emissions which are associated with such processes. Methods are needed that accomplish environmental stewardship, yet still provide high-volume cost-effective oil production.\|[0005] Below ground in-situ concepts emerged based on their ability to produce high volumes while avoiding the cost of mining. While the cost savings resulting from avoiding mining can be achieved, the in-situ method requires heating a formation for a longer period of time due to the extremely low thermal conductivity and high specific heat of solid oil shale. Perhaps the most significant challenge for any in-situ process is the uncertainty and long term potential of water contamination that can occur with underground freshwater aquifers. In the case of Shell's ICP method, a “freeze wall” is used as a barrier to keep separation between aquifers and an underground treatment area. Although this is possible, no long term analysis has proven for extended periods to guarantee the prevention of contamination. Without guarantees and with even fewer remedies should a freeze wall fail, other methods are desirable to address such environmental risks.\|[0006] For this and other reasons, the need remains for methods and systems which can provide improved recovery of hydrocarbons from suitable hydrocarbon-containing materials, which have acceptable economics and avoid the drawbacks mentioned above.\|SUMMARY\|[0007] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating the hydrocarbonaceous material can be substantially stationary. Additionally, during heating, any carbon dioxide that is produced can be sequestered. Removed hydrocarbons can be collected for further processing, use in the process as supplemental fuel or additives, and/or direct use without further treatment.\|[0008] Additional features and advantages of these principles will be apparent from the following detailed description, which illustrates, by way of example, features of the invention.\|(US8323481)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0009] FIG. 1 is side partial cutaway view schematic of a constructed permeability control infrastructure in accordance with one embodiment.\|[0010] FIGS. 2A and 2B are top and plan views of a plurality of permeability control impoundments in accordance with one embodiment.\|[0011] FIG. 3 is a side cutaway view of a permeability control impoundment in accordance with one embodiment.\|[0012] FIG. 4 is a schematic of a portion of a constructed infrastructure in accordance with an embodiment.\|[0013] FIG. 5 is a schematic showing heat transfer between two permeability control impoundments in accordance with another embodiment.\|(US8323481)\|DETAILED DESCRIPTION\|[0014] It should be noted that the figures are merely exemplary of several embodiments and no limitations on the scope of the present invention are intended thereby. Further, the figures are generally not drawn to scale, but are drafted for purposes of convenience and clarity in illustrating various aspects of the invention.\|DETAILED DESCRIPTION\|[0015] Reference will now be made to exemplary embodiments and specific language will be used herein to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended. Alterations and further modifications of the inventive features described herein, and additional applications of the principles of the invention as described herein, which would occur to one skilled in the relevant art and having possession of this disclosure, are to be considered within the scope of the invention. Further, before particular embodiments are disclosed and described, it is to be understood that this invention is not limited to the particular process and materials disclosed herein as such may vary to some degree. It is also to be understood that the terminology used herein is used for the purpose of describing particular embodiments only and is not intended to be limiting, as the scope of the present invention will be defined only by the appended claims and equivalents thereof.\|DEFINITIONS\|[0016] In describing and claiming the present invention, the following terminology will be used.\|[0017] The singular forms “a,” “an,” and “the” include plural references unless the context clearly dictates otherwise. Thus, for example, reference to “a wall” includes reference to one or more of such structures, “a permeable body” includes reference to one or more of such materials, and “a heating step” refers to one or more of such steps.\|[0018] As used herein “existing grade” or similar terminology refers to the grade or a plane parallel to the local surface topography of a site containing an infrastructure as described herein which infrastructure may be above or below the existing grade.\|[0019] As used herein, “conduits” refers to any passageway along a specified distance which can be used to transport materials and/or heat from one point to another point. Although conduits can generally be circular pipes, other non-circular conduits can also be useful. Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|[0020] As used herein, “constructed infrastructure” refers to a structure which is substantially entirely man made, as opposed to freeze walls, sulfur walls, or other barriers which are formed by modification or filling pores of an existing geological formation.\|[0021] The constructed permeability control infrastructure is often substantially free of undisturbed geological formations, although the infrastructure can be formed adjacent or in direct contact with an undisturbed formation. Such a control infrastructure can be unattached or affixed to an undisturbed formation by mechanical means, chemical means, or a combination of such means, e.g. bolted into the formation using anchors, ties, or other suitable hardware.\|[0022] As used herein, “comminuted” refers to breaking a formation or larger mass into pieces. A comminuted mass can be rubbilized or otherwise broken into fragments.\|[0023] As used herein, “hydrocarbonaceous material” refers to any hydrocarbon-containing material from which hydrocarbon products can be extracted or derived. For example, hydrocarbons may be extracted directly as a liquid, removed via solvent extraction, directly vaporized or otherwise removed from the material. However, many hydro carbonaceous materials contain kerogen or bitumen which is converted to a hydrocarbon through heating and pyrolysis. Hydrocarbonaceous materials can include, but is not limited to, oil shale, tar sands, coal, lignite, bitumen, peat, and other organic materials.\|[0024] As used herein, “impoundment” refers to a structure designed to hold or retain an accumulation of fluid and/or solid moveable materials. An impoundment generally derives at least a substantial portion of foundation and structural support from earthen materials. Thus, the control walls do not always have independent strength or structural integrity apart from the earthen material and/or formation against which they are formed.\|[0025] As used herein, “permeable body” refers to any mass of comminuted hydro carbonaceous material having a relatively high permeability which exceeds permeability of a solid undisturbed formation of the same composition. Suitable permeable bodies can have greater than about 10% void space and typically have void space from about 30% to 45%, although other ranges may be suitable. Allowing for high permeability facilitates, for example, through the incorporation of large irregularly shaped particles, heating of the body through convection as the primary heat transfer while also substantially reducing costs associated with crushing to very small sizes, e.g. below about 1 to about 0.5 inch.\|[0026] As used herein, “wall” refers to any constructed feature having a permeability control contribution to confining material within an encapsulated volume defined at least in part by control walls. Walls can be oriented in any manner such as vertical, although ceilings, floors, and other contours defining the encapsulated volume can also be “walls” as used herein.\|[0027] As used herein, “mined” refers to a material which has been removed or disturbed from an original stratographic or geological location to a second and different location or returned to the same location. Typically, mined material can be produced by rubbilizing, crushing, explosively detonating, or otherwise removing material from a geologic formation.\|[0028] As used herein, “adsorb,” “adsorbing,” or “adsorbed” refers to the process where a gas or liquid solute accumulates on the surface of a solid or a liquid or diffuses into a solid or liquid. Generally, when referring to carbon dioxide, the carbon dioxide is adsorbed into a material such that the carbon dioxide is substantially immobilized.\|[0029] As used herein, “substantially stationary” refers to nearly stationary positioning of materials with a degree of allowance for subsidence, expansion, and/or settling as hydrocarbons are removed from the hydrocarbonaceous material from within the enclosed volume to leave behind lean material. In contrast, any circulation and/or flow of hydrocarbonaceous material such as that found in fluidized beds or rotating retorts involves highly substantial movement and handling of hydrocarbonaceous material.\|[0030] As used herein, “substantial” when used in reference to a quantity or amount of a material, or a specific characteristic thereof, refers to an amount that is sufficient to provide an effect that the material or characteristic was intended to provide. The exact degree of deviation allowable may in some cases depend on the specific context. Similarly, “substantially free of” or the like refers to the lack of an identified element or agent in a composition. Particularly, elements that are identified as being “substantially free of” are either completely absent from the composition, or are included only in amounts which are small enough so as to have no measurable effect on the composition.\|[0031] As used herein, “about” refers to a degree of deviation based on experimental error typical for the particular property identified. The latitude provided the term “about” will depend on the specific context and particular property and can be readily discerned by those skilled in the art. The term “about” is not intended to either expand or limit the degree of equivalents which may otherwise be afforded a particular value. Further, unless otherwise stated, the term “about” shall expressly include “exactly,” consistent with the discussion below regarding ranges and numerical data.\|[0032] Concentrations, dimensions, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of about 1 to about 200 should be interpreted to include not only the explicitly recited limits of 1 and 200, but also to include individual sizes such as 2, 3, 4, and sub-ranges such as 10 to 50, 20 to 100, etc.\|[0033] As used herein, a plurality of items, structural elements, compositional elements, and/or materials may be presented in a common list for convenience. However, these lists should be construed as though each member of the list is individually identified as a separate and unique member. Thus, no individual member of such list should be construed as a de facto equivalent of any other member of the same list solely based on their presentation in a common group without indications to the contrary.\|[0034] Carbon Management and Sequestration from Control Infrastructures\|[0035] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined or harvested hydro carbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure is a fixed structure. Additionally, during heating, at least a portion of carbon dioxide that is produced can be sequestered. Removed fluid hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.\|[0036] The constructed permeability control infrastructure can be formed using existing grade as floor support and/or as side wall support for the constructed infrastructure. For example, the control infrastructure can be formed as a free standing structure, i.e. using only existing grade as a floor with side walls being man-made. Alternatively, the control infrastructure can be formed within an excavated pit. Regardless, the control infrastructures are always formed above-grade.\|[0037] A constructed permeability control infrastructure can include a permeability control impoundment which defines a substantially encapsulated volume. The permeability control impoundment is substantially free of undisturbed geological formations. Specifically, the permeability control aspect of the impoundment can be completely constructed and manmade as a separate isolation mechanism for prevention of uncontrolled migration of material into or out of the encapsulated volume.\|[0038] In one embodiment, the permeability control impoundment can be formed along walls of an excavated hydrocarbonaceous material deposit. For example, oil shale, tar sands, or coal can be mined from a deposit to form a cavity which corresponds approximately to a desired encapsulation volume for an impoundment. The excavated cavity can then be used as a form and support to create the permeability control impoundment.\|[0039] In one alternative aspect, at least one additional excavated hydrocarbonaceous material deposit can be formed such that a plurality of impoundments can be operated. Further, such a configuration can facilitate a reduction in transportation distance of the mined material. Specifically, the mined hydro carbonaceous material for any particular encapsulated volume can be mined from an adjacent excavated hydrocarbonaceous material deposit. In this manner, a grid of constructed structures can be built such that mined material can be immediately and directly filled into an adjacent impoundment.\|[0040] Mining and/or excavation of hydrocarbonaceous deposits can be accomplished using any suitable technique. Conventional surface mining can be used, although alternative excavators can also be used without requirement of transportation of the mined materials. In one specific embodiment, the hydrocarbonaceous deposit can be excavated using a crane-suspended excavator. One example of a suitable excavator can include vertical tunnel boring machines. Such machines can be configured to excavate rock and material beneath the excavator. As material is removed, the excavator is lowered to ensure substantially continuous contact with a formation. Removed material can be conveyed out of the excavation area using conveyors or lifts. Alternatively, the excavation can occur under aqueous slurry conditions to reduce dust problems and act as a lubricant/coolant. The slurry material can be pumped out of the excavation for separation of solids in a settling tank or other similar solid-liquid separator, or the solids may be allowed to precipitate directly in an impoundment. This approach can be readily integrated with simultaneous or sequential solution-based recovery of metals and other materials as described in more detail below.\|[0041] Further, excavation and formation of a permeability control impoundment can be accomplished simultaneously. For example, an excavator can be configured to remove hydrocarbonaceous material while side walls of an impoundment are formed. Material can be removed from just underneath edges of the side walls such that the walls can be guided downward to allow additional wall segments to be stacked above. This approach can allow for increased depths while avoiding or reducing dangers of cave-in prior to formation of supporting impoundment walls.\|[0042] The impoundment can be formed of any suitable material which provides isolation of material transfer across walls of the impoundment. In this manner, integrity of the walls is retained during operation of the control infrastructure sufficient to substantially prevent uncontrolled migration of fluids outside of the control infrastructure. Non-limiting examples of suitable material for use in forming the impoundment of the constructed permeability control infrastructure can include clay, bentonite clay (e.g. clay comprising at least a portion of bentonite), bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, or combinations thereof. Engineered cementitious composites (ECC) materials, fiber reinforced composites, and the like can be particularly strong and can be readily engineered to meet permeability and temperature tolerance requirements of a given installation. As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required. For example, materials having a melting point above the maximum operating temperature of the infrastructure can be useful to maintain containment during and after heating and recovery. However, lower temperature materials can also be used if a non-heated buffer zone is maintained between the walls and heated portions of the permeable body. Such buffer zones can range from 6 inches to 50 feet depending on the particular material used for the impoundment and the composition of the permeable body. In another aspect, walls of the impoundment can be acid, water, and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water. For impoundment walls formed along formations or other solid support, the impoundment walls can be formed of a sprayed grouting, sprayed liquid emulsions, or other sprayed material such as sprayable refractory grade grouting which forms a seal against the formation and creates the permeability control wall of the impoundments. Impoundment walls may be substantially continuous such that the impoundment defines the encapsulated volume sufficiently to prevent substantial movement of fluids into or out of the impoundment other than defined inlets and outlets, e.g. via conduits or the like as discussed herein. In this manner, the impoundments can readily meet government fluid migration regulations. Alternatively, or in combination with a manufactured barrier, portions of the impoundment walls can be undisturbed geological formation and/or compacted earth. In such cases, the constructed permeability control infrastructure is a combination of permeable and impermeable walls as described in more detail below.\|[0043] In one detailed aspect, a portion of hydro carbonaceous material, either pre- or post-processed, can be used as a cement fortification and/or cement base which are then poured in place to form portions or the entirety of walls of the control infrastructure. These materials can be formed in place or can be preformed and then assembled on site to form an integral impoundment structure. For example, the impoundment can be constructed by cast forming in place as a monolithic body, extrusion, stacking of preformed or precast pieces, concrete panels joined by a grout (cement, ECC, or other suitable material), inflated form, or the like. The forms can be built up against a formation or can be stand alone structures. Forms can be constructed of any suitable material such as, but not limited to, steel, wood, fiberglass, polymer, or the like. The forms can be assembled in place or may be oriented using a crane or other suitable mechanism. Alternatively, the constructed permeability control infrastructure can be formed of gabions and/or geosynthetic fabrics assembled in layers with compacted fill material. Optional binders can be added to enhance compaction of the permeability control walls. In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|[0044] Impoundment walls can optionally include non-permeable insulation and/or fines collection layers. These permeable layers can be oriented between the permeability control barrier and the permeable body. For example, a layer of hydrocarbonaceous comminuted material can be provided which allows fluids to enter, cool, and at least partially condense within the layer. Such permeable layer material can generally have a particle size smaller than the permeable body. Further, such hydrocarbonaceous material can remove fines from passing fluids via various attractive forces. In one embodiment, the construction of impoundment walls and floors can include multiple compacted layers of indigenous or manipulated low grade shale with any combination of sand, cement, fiber, plant fiber, nano carbons, crushed glass, reinforcement steel, engineered carbon reinforcement grid, calcium salts, and the like. In addition to such composite walls, designs which inhibit long term fluid and gas migration through additional impermeability engineering can be employed including, but not limited to, liners, geo-membranes, compacted soils, imported sand, gravel or rock and gravity drainage contours to move fluids and gases away from impervious layers to egress exits. Impoundment floor and wall construction, can, but need not comprise, a stepped up or stepped down slope or bench as the case of mining course may dictate following the optimal ore grade mining. In any such stepped up or down applications, floor leveling and containment wall construction can typically drain or slope to one side or to a specific central gathering area(s) for removal of fluids by gravity drainage assistance.\|[0045] Optionally, capsule wall and floor construction can include insulation which prevents heat transfer outside of the constructed infrastructure or outside of inner capsules or conduits within the primary constructed capsule containment. Insulation can comprise manufactured materials, cement or various materials other materials which are less thermally conductive than surrounding masses, i.e. permeable body, formation, adjacent infrastructures, etc. Thermally insulating barriers can also be formed within the permeable body, along impoundment walls, ceilings, and/or floors. One detailed aspect includes the use of biodegradable insulating materials, e.g. soy insulation and the like. This is consistent with embodiments wherein the impoundment is a single use system such that insulations, pipes, and/or other components can have a relatively low useful life, e.g. less than 1-2 years. This can reduce equipment costs as well as reduce long-term environmental impact.\|[0046] These structures and methods can be applied at almost any scale. Larger encapsulated volumes and increased numbers of impoundments can readily produce hydrocarbon products and performance comparable to or exceeding smaller constructed infrastructures. As an illustration, single impoundments can range in size from tens of meters across to tens of acres. Optimal impoundment sizes may vary depending on the hydrocarbonaceous material and operating parameters, however it is expected that suitable areas can range from about one-half to five acres in top plan surface area.\|[0047] The methods and infrastructures can be used for recovery of hydrocarbons from a variety of hydrocarbonaceous materials. One particular advantage is a wide degree of latitude in controlling particle size, conditions, and composition of the permeable body introduced into the encapsulated volume. Non-limiting examples of mined hydrocarbonaceous material which can be treated comprise oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof. In some cases it can be desirable to provide a single type of hydro carbonaceous material so that the permeable body consists essentially of one of the above materials. However, the permeable body can include mixtures of these materials such that grade, oil content, hydrogen content, permeability and the like can be adjusted to achieve a desired result. Further, different hydrocarbon materials can be placed in multiple layers or in a mixed fashion such as combining coal, oil shale, tar sands, biomass, and/or peat.\|[0048] In one embodiment, hydrocarbon containing material can be classified into various inner capsules within a primary constructed infrastructure for optimization reasons. For instance, layers and depths of mined oil shale formations may be richer in certain depth pay zones as they are mined. Once blasted, mined, shoveled, and hauled inside of capsule for placement, richer oil bearing ores can be classified or mixed by richness for optimal yields, faster recovery, or for optimal averaging within each impoundment. Further, providing layers of differing composition can have added benefits. For example, a lower layer of tar sands can be oriented below an upper layer of oil shale. Generally, the upper and lower layers can be in direct contact with one another although this is not required. The upper layer can include heating pipes embedded therein as described in more detail below. The heating pipes can heat the oil shale sufficient to liberate kerogen oil, including short-chain liquid hydrocarbons, which can act as a solvent for bitumen removal from the tar sands. In this manner, the upper layer acts as an in situ solvent source for enhancing bitumen removal from the lower layer. Heating pipes within the lower layer are optional such that the lower layer can be free of heating pipes or may include heating pipes, depending on the amount of heat transferred via downward passing liquids from the upper layer and any other heat sources. The ability to selectively control the characteristics and composition of the permeable body adds a significant amount of freedom in optimizing oil yields and quality.\|[0049] Furthermore, in many embodiments, the liberated gaseous and liquid products act as an in situ produced solvent which supplements kerogen removal and/or additional hydrocarbon removal from the hydrocarbonaceous material.\|[0050] In yet another detailed aspect, the permeable body can further comprise an additive or biomass. Additives can include any composition which acts to increase the quality of removed hydrocarbons, e.g. increased API, decreased viscosity, improved flow properties, reduced wetting of residual shale, reduction of sulfur, hydrogenation agents, etc. Non-limiting examples of suitable additives can include bitumen, kerogen, propane, natural gas, natural gas condensate, crude oil, refining bottoms, asphaltenes, common solvents, other diluents, and combinations of these materials. In one specific embodiment, the additive can include a flow improvement agent and/or a hydrogen donor agent. Some materials can act as both or either agents to improve flow or as a hydrogen donor. Non-limiting examples of such additives can include methane, natural gas condensates, common solvent such as acetone, toluene, benzene, etc., and other additives listed above. Additives can act to increase the hydrogen to carbon ratio in any hydrocarbon products, as well as act as a flow enhancement agent. For example, various solvents and other additives can create a physical mixture which has a reduced viscosity and/or reduced affinity for particulate solids, rock, and the like. Further, some additives can chemically react with hydrocarbons and/or allow liquid flow of the hydrocarbon products. Any additives used can become part of a final recovered product or can be removed and reused or otherwise disposed of.\|[0051] Similarly, biological hydroxylation of hydrocarbonaceous materials to form synthetic gas or other lighter weight products can be accomplished using known additives and approaches. Enzymes or biocatalysts can also be used in a similar manner. Further, manmade materials can also be used as additives such as, but not limited to, tires, polymeric refuse, or other hydrocarbon-containing materials.\|[0052] Although these methods are broadly applicable, as a general guideline, the permeable body can include particles from about ⅛ inch to about 6 feet in largest dimension, and in some cases less than 1 foot and in other cases less than about 6 inches. However, as a practical matter, sizes from about 2 inches to about 2 feet can provide good results with about 1 foot diameter being useful for oil shale especially. Void space can be an important factor in determining optimal particle diameters. As a general matter, any functional void space can be used; however, about 10% to about 50% and in some cases about 30% to about 45% usually provides a good balance of permeability and effective use of available volumes. Void volumes can be varied somewhat by varying other parameters such as heating conduit placement, additives, and the like. Mechanical separation of mined hydrocarbonaceous materials allows creation of fine mesh, high permeability particles which enhance thermal dispersion rates once placed in capsule within the impoundment. The added permeability allows for more reasonable, low temperatures which also help to avoid higher temperatures which result in greater CO2 production from carbonate decomposition and associated release of trace heavy metals, volatile organics, and other compounds which can create toxic effluent and/or undesirable materials which are monitored and controlled.\|[0053] Carbon dioxide that is produced during the recovery process can be sequestered using one or more approaches. In particular, carbon dioxide can be converted to a solid or liquid form such that the associated carbon is precipitated or otherwise converted to a useful product. Such sequestering can be optionally accomplished by reacting carbon dioxide with an aqueous solution to form a precipitation of carbon dioxide with a metal. When referring to carbon dioxide precipitates or precipitating carbon dioxide, it is understood that precipitation consumes the carbon dioxide such that the carbon dioxide no longer exists as a CO2 structure. As such, the process is generally irreversible and differs from general adsorption techniques, which can also be used for sequestering carbon dioxide as further described herein. In one embodiment, the aqueous solution can be an ionic solution. In another embodiment, the aqueous solution can be salt water. The metal can be any metal that is capable of forming a solid with carbon dioxide including oxides thereof. In one embodiment, the metal can be calcium, magnesium, including oxides thereof, silicates thereof, and mixtures thereof. In one embodiment, the metal can be in the form of forsterite, serpentine and/or peridotite. In one embodiment, the exhausted hydrocarbonaceous materials can be injected or admixed with the carbon dioxide and salt water to form carbon dioxide precipitates. Such a process can take advantage of metals found in the exhausted hydrocarbonaceous materials.\|[0054] Additionally, other materials can be added to increase the reaction kinetics to form the carbon dioxide precipitate. For example, the addition of acids, catalysts, or other organic compounds may increase the reaction kinetics. Such sequestering can also produce heat during the sequestering process. In one embodiment, the heat can be redirected and applied to the heating step as discussed herein. Such recycling of heat can further provide a more efficient recovery system.\|[0055] Additionally, or alternatively, sequestering of carbon dioxide can be achieved by cryogenic precipitation forming liquid carbon dioxide. The collected carbon dioxide can be liquefied by lowering the temperature. Such liquid carbon dioxide can then be transferred to a container for disposal or for reuse. In one embodiment, the liquid carbon dioxide can be reacted to form polycarbonates, which can provide a stable form for disposal or potential use in other industries. In another embodiment, the liquid carbon dioxide can be used to further process the exhausted hydrocarbonaceous materials, as further discussed herein, including rinsing the hydrocarbonaceous materials during the recovery process. Such treatment can provide additional recovery of hydrocarbons that have not been removed during the initial recovery process as described herein.\|[0056] The sequestered carbon dioxide can be used in other commercial processes. In one embodiment, carbon dioxide can be used to isolate polymers from fluids. For example, carbon dioxide can be used to isolate polycarbonates from a solvent, e.g. methylene chloride. In another embodiment, carbon dioxide can be pumped into depleted permeable bodies. In the case of permeable bodies having a high coal content, once the initial stores of methane or other products are recovered, CO2 can be pumped into the impoundment, where it is stored in the coal, which can then provide the benefit of releasing additional methane. Between three and thirteen molecules of CO2 can be absorbed for each molecule of methane, making coal an excellent storage location for CO2.\|[0057] In one embodiment, storage of carbon dioxide can be performed in deep saline aquifers or brine-saturated rock formations that occur deep underground or under the ocean. Specifically, wells deep underground consisting of porous rock, such as limestone or sandstone, saturated with saltwater can form an effective trap for injected CO2. Geologically, over time, some CO2 can react with rock minerals to form solid carbonates, further immobilizing the same.\|[0058] Additionally, a liquid carbon dioxide can be optionally mixed and/or adsorbed by the exhausted hydrocarbonaceous materials. Such materials can then be disposed in an appropriate manner. When referring to liquid carbon dioxide, the embodiments herein can also be used with supercritical carbon dioxide. As such, the discussion and embodiments presented herein referring to liquid carbon dioxide also can be applied with respect to supercritical carbon dioxide.\|[0059] In another embodiment, sequestering carbon dioxide can be achieved by injecting exhausted hydrocarbonaceous materials with the carbon dioxide. Such injection can provide adsorption of carbon dioxide. Additionally, such process can be performed with a catalyst or without a catalyst. Other metal and organic additives can be included as discussed herein. In one embodiment, such sequestering can include a metal selected from the group consisting of calcium, magnesium, including oxides thereof, silicates thereof, and mixtures thereof.\|[0060] With respect to carbon dioxide sequestering, a constructed permeability control infrastructure can comprise a permeability control impoundment defining a substantially encapsulated volume wherein the permeability control impoundment is substantially free of undisturbed geological formations, a comminuted hydrocarbonaceous material within the encapsulated volume forming a permeable body of hydrocarbonaceous material, and a carbon dioxide collection unit operatively connected to collect carbon dioxide from the control infrastructure. It is understood that the infrastructure can include any of the elements described herein including those elements that have been referred to in the context of a process. Additionally, the methods and processes described herein can include any elements described herein including those elements that have been referred to in the context of a composition or system.\|[0061] The carbon dioxide can be collected consistent with one or more of the above approaches using a corresponding carbon dioxide control unit. In one optional aspect, the carbon dioxide control unit can include a vessel for treatment and/or storage of the carbon dioxide. Additional storage tanks, pumps and/or vessels can also be used for transporting or storage of treatment chemicals and by-products. As described herein, the vessel can contain an aqueous solution, a metal, and carbon dioxide where the vessel is configured to react the carbon dioxide with the aqueous solution to form a precipitation of carbon dioxide with the metal. In another embodiment, the vessel can contain carbon dioxide where the vessel is configured to form liquid carbon dioxide from the carbon dioxide by cryogenic precipitation. Additionally, the vessel can contain exhausted hydrocarbonaceous materials that adsorb the liquid carbon dioxide. In one embodiment, the vessel can contain carbon dioxide where the vessel is configured to mix exhausted hydrocarbonaceous materials with the carbon dioxide such that the exhausted hydrocarbonaceous materials adsorb the carbon dioxide.\|[0062] In one embodiment, computer assisted mining, mine planning, hauling, blasting, assay, loading, transport, placement, and dust control measures can be utilized to fill and optimize the speed of mined material movement into the constructed capsule containment structure. In one alternative aspect, the impoundments can be formed in excavated volumes of a hydrocarbonaceous formation, although other locations remote from the control infrastructure can also be useful. For example, some hydrocarbonaceous formations have relatively thin hydrocarbon-rich layers, e.g. less than about 300 feet thick. Therefore, vertical mining and drilling tend to not be cost effective. In such cases, horizontal mining can be useful to recover the hydrocarbonaceous materials for formation of the permeable body. Although horizontal mining continues to be a challenging endeavor, a number of technologies have been developed and continue to be developed which can be useful in connection with the impoundments. In such cases, at least a portion of the impoundment can be formed across a horizontal layer, while other portions of the impoundment can be formed along and/or adjacent non-hydrocarbon bearing formation layers. Other mining approaches such as, but not limited to, room and pillar mining can provide an effective source of hydrocarbonaceous material with minimal waste and/or reclamation which can be transported to an impoundment and treated in accordance with the these principles.\|[0063] As mentioned herein, these systems and processes allow for a large degree of control regarding properties and characteristics of the permeable body which can be designed and optimized for a given installation. Impoundments, individually and across a plurality of impoundments can be readily tailored and classified based on varying composition of materials, intended products and the like. For example, several impoundments can be dedicated to production of heavy crude oil, while others can be configured for production of lighter products and/or syn gas. Non-limiting example of potential classifications and factors can include catalyst activity, enzymatic reaction for specific products, aromatic compounds, hydrogen content, microorganism strain or purpose, upgrading process, target final product, pressure (effects product quality and type), temperature, swelling behavior, aquathermal reactions, hydrogen donor agents, heat superdisposition, garbage impoundment, sewage impoundment, reusable pipes, and others. Typically, a plurality of these factors can be used to configure impoundments in a given project area for distinct products and purposes.\|[0064] The comminuted hydrocarbonaceous material can be filled into the control infrastructure to form the permeable body in any suitable manner. Typically the comminuted hydrocarbonaceous material can be conveyed into the control infrastructure by dumping, conveyors or other suitable approaches. As mentioned previously, the permeable body can have a suitably high void volume. Indiscriminate dumping can result in excessive compaction and reduction of void volumes. Thus, the permeable body can be formed by low compaction conveying of the hydrocarbonaceous material into the infrastructure. For example, retracting conveyors can be used to deliver the material near a top surface of the permeable body as it is formed. In this way, the hydrocarbonaceous material can retain a significant void volume between particles without substantial further crushing or compaction despite some small degree of compaction which often results from lithostatic pressure as the permeable body is formed.\|[0065] Once a desired permeable body has been formed within the control infrastructure, heat can be introduced sufficient to begin removal of hydrocarbons, e.g. via pyrolysis. A suitable heat source can be thermally associated with the permeable body. Optimal operating temperatures within the permeable body can vary depending on the composition and desired products. However, as a general guideline, operating temperatures can range from about 200° F. to about 750° F. Temperature variations throughout the encapsulated volume can vary and may reach as high as 900° F. or more in some areas. In one embodiment, the operating temperature can be a relatively lower temperature to facilitate production of liquid product such as from about 200° F. to about 650° F. This heating step can be a roasting operation which results in beneficiation of the crushed ore of the permeable body. Further, one embodiment comprises controlling the temperature, pressure and other variables sufficient to produce predominantly, and in some cases substantially only, liquid product. Generally, products can include both liquid and gaseous products, while liquid products can require fewer processing steps such as scrubbers etc. The relatively high permeability of the permeable body allows for production of liquid hydrocarbon products and minimization of gaseous products, depending to some extent on the particular starting materials and operating conditions. In one embodiment, the recovery of hydrocarbon products can occur substantially in the absence of cracking within the permeable body.\|[0066] In one aspect, heat can be transferred to the permeable body via convection. Heated gases can be injected into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body. Heated gases can be produced by combustion of natural gas, hydrocarbon product, or any other suitable source. Non-limiting examples of suitable heat transfer fluids can include hot air, hot exhaust gases, steam, hydrocarbon vapors and/or hot liquids. The heated gases can be imported from external sources or recovered from the process.\|[0067] Alternatively, or in combination with convective heating, a highly configurable approach can include embedding a plurality of conduits within the permeable body. The conduits can be configured for use as heating pipes, cooling pipes, heat transfer pipes, drainage pipes, or gas pipes. Further, the conduits can be dedicated to a single function or may serve multiple functions during operation of the infrastructure, i.e. heat transfer and drainage. The conduits can be formed of any suitable material, depending on the intended function. Non-limiting examples of suitable materials can include clay pipes, refractory cement pipes, refractory ECC pipes, poured in place pipes, metal pipes such as cast iron, stainless steel etc., polymer such as PVC, and the like. In one specific embodiment, all or at least a portion of the embedded conduits can comprise a degradable material. For example, non-galvanized 6″ cast iron pipes can be effectively used for single use embodiments and perform well over the useful life of the impoundment, typically less than about 2 years. Further, different portions of the plurality of conduits can be formed of different materials. Poured in place pipes can be especially useful for very large encapsulation volumes where pipe diameters exceed several feet. Such pipes can be formed using flexible wraps which retain a viscous fluid in an annular shape. For example, PVC pipes can be used as a portion of a form along with flexible wraps, where concrete or other viscous fluid is pumped into an annular space between the PVC and flexible wrap. Depending on the intended function, perforations or other apertures can be made in the conduits to allow fluids to flow between the conduits and the permeable body. Typical operating temperatures exceed the melting point of conventional polymer and resin pipes. In some embodiments, the conduits can be placed and oriented such that the conduits intentionally melt or otherwise degrade during operation of the infrastructure.\|[0068] The plurality of conduits can be readily oriented in any configuration, whether substantially horizontal, vertical, slanted, branched, or the like. At least a portion of the conduits can be oriented along predetermined pathways prior to embedding the conduits within the permeable body. The predetermined pathways can be designed to improve heat transfer, gas-liquid-solid contacting, maximize fluid delivery or removal from specific regions within the encapsulated volume, or the like. Further, at least a portion the conduits can be dedicated to heating of the permeable body. These heating conduits can be selectively perforated to allow heated gases or other fluids to convectively heat and mix throughout the permeable body. The perforations can be located and sized to optimize even and/or controlled heating throughout the permeable body. Alternatively, the heating conduits can form a closed loop such that heating gases or fluids are segregated from the permeable body. Thus, a “closed loop” does not necessarily require recirculation, rather isolation of heating fluid from the permeable body. In this manner, heating can be accomplished primarily or substantially only through thermal conduction across the conduit walls from the heating fluids into the permeable body. Heating in a closed loop allows for prevention of mass transfer between the heating fluid and permeable body and can reduce formation and/or extraction of gaseous hydrocarbon products.\|[0069] During the heating or roasting of the permeable body, localized areas of heat which exceed parent rock decomposition temperatures, often above about 900° F., can reduce yields and form carbon dioxide and undesirable contaminating compounds which can lead to leachates containing heavy metals, soluble organics and the like. The heating conduits can allow for substantial elimination of such localized hot spots while maintaining a vast majority of the permeable body within a desired temperature range. The degree of uniformity in temperature can be a balance of cost (e.g. for additional heating conduits) versus yields. However, at least about 85% of the permeable body can readily be maintained within about 5-10% of a target temperature range with substantially no hot spots, i.e. exceeding the decomposition temperature of the hydrocarbonaceous materials such as about 800° F. and in many cases about 900° F. Thus, operated as described herein, the systems can allow for recovery of hydrocarbons while eliminating or substantially avoiding production of undesirable leachates. Although products can vary considerably depending on the starting materials, high quality liquid and gaseous products are possible. In accordance with one embodiment, a crushed oil shale material can produce a liquid product having an API from about 30 to about 45, with about 33 to about 38 being currently typical, directly from the oil shale without additional treatment. Interestingly, practice of these processes has led to an understanding that pressure appears to be a much less influential factor on the quality of recovered hydrocarbons than temperature and heating times. Although heating times can vary considerably, depending on void space, permeable body composition, quality, etc., as a general guideline times can range from a few days (i.e. 3-4 days) up to about one year. In one specific example, heating times can range from about 2 weeks to about 4 months. Under-heating oil shale at short residence times, i.e. minutes to several hours, can lead to formation of leachable and/or somewhat volatile hydrocarbons. Accordingly, these systems and methods allow for extended residence times at moderate temperatures such that organics present in oil shale can be volatilized and/or carbonized, leaving insubstantial leachable organics. In addition, the underlying shale is not generally decomposed or altered which reduces soluble salt formation.\|[0070] Further, conduits can be oriented among a plurality of impoundments and/or control infrastructures to transfer fluids and/or heat between the structures. The conduits can be welded to one another using conventional welding or the like. Further, the conduits can include junctions which allow for rotation and or small amounts of movement during expansion and subsidence of material in the permeable body. Additionally, the conduits can include a support system which acts to support the assembly of conduits prior to and during filling of the encapsulated volume, as well as during operation. For example, during heating flows of fluids, heating and the like can cause expansion (fracturing or popcorn effect) or subsidence sufficient to create potentially damaging stress and strain on the conduits and associated junctions. A truss support system or other similar anchoring members can be useful in reducing damage to the conduits. The anchoring members can include cement blocks, 1-beams, rebar, columns, etc. which can be associated with walls of the impoundment, including side walls, floors and ceilings.\|[0071] Alternatively, the conduits can be completely constructed and assembled prior to introduction of any mined materials into the encapsulated volume. Care and planning can be considered in designing the predetermined pathways of the conduits and method of filling the volume in order to prevent damage to the conduits during the filling process as the conduits are buried. Thus, as a general rule, the conduits are oriented ab initio, or prior to embedding in the permeable body such that they are non-drilled. As a result, construction of the conduits and placement thereof can be performed without extensive core drilling and/or complicated machinery associated with well-bore or horizontal drilling. Rather, horizontal or any other orientation of conduit can be readily achieved by assembling the desired predetermined pathways prior to, or contemporaneous with, filling the infrastructure with the mined hydrocarbonaceous material. The non-drilled, hand/crane-placed conduits oriented in various geometric patterns can be laid with valve controlled connecting points which yield precise and closely monitored heating within the capsule impoundment. The ability to place and layer conduits including connecting, bypass and flow valves, and direct injection and exit points, allow for precision temperature and heating rates, precision pressure and pressurization rates, and precision fluid and gas ingress, egress and composition admixtures. For example, when a bacteria, enzyme, or other biological material is used, optimal temperatures can be readily maintained throughout the permeable body to increase performance, reaction, and reliability of such biomaterials.\|[0072] The conduits will generally pass through walls of the constructed infrastructure at various points. Due to temperature differences and tolerances, it can be beneficial to include an insulating material at the interface between the wall and the conduits. The dimensions of this interface can be minimized while also allowing space for thermal expansion differences during startup, steady-state operation, fluctuating operating conditions, and shutdown of the infrastructure. The interface can also involve insulating materials and sealant devices which prevent uncontrolled egress of hydrocarbons or other materials from the control infrastructure. Non-limiting examples of suitable materials can include high temperature gaskets, metal alloys, ceramics, clay or mineral liners, composites or other materials which having melting points above typical operating temperatures and act as a continuation of the permeability control provided by walls of the control infrastructure.\|[0073] Further, walls of the constructed infrastructure can be configured to minimize heat loss. In one aspect, the walls can be constructed having a substantially uniform thickness which is optimized to provide sufficient mechanical strength while also minimizing the volume of wall material through which the conduits pass. Specifically, excessively thick walls can reduce the amount of heat which is transferred into the permeable body by absorbing the same through conduction. Conversely, the walls can also act as a thermal barrier to somewhat insulate the permeable body and retain heat therein during operation.\|[0074] In one embodiment, fluid and gas compounds within the permeable body can be altered for desired extractive products using, as an example, induced pressure through gases or piled lithostatic pressure from piled rubble. Thus, some degree of upgrading and/or modification can be accomplished simultaneous with the recovery process. Further, certain hydro carbonaceous materials can require treatment using specific diluents or other materials. For example, treatment of tar sands can be readily accomplished by steam injection or solvent injection to facilitate separation of bitumen from sand particles according to well known mechanisms.\|[0075] With the above description in mind, FIG. 1 depicts a side view of one embodiment showing an engineered capsule containment and extraction impoundment 100 where existing grade 108 is used primarily as support for the impermeable floor layer 112. Exterior capsule impoundment side walls 102 provide containment and can, but need not be, subdivided by interior walls 104. Subdividing can create separate containment capsules 122 within a greater capsule containment of the impoundment 100 which can be any geometry, size or subdivision. Further subdivisions can be horizontally or vertically stacked. By creating separate containment capsules 122 or chambers, classification of lower grade materials, varied gases, varied liquids, varied process stages, varied enzymes or microbiology types, or other desired and staged processes can be readily accommodated. Sectioned capsules constructed as silos within larger constructed capsules can also be designed to provide staged and sequenced processing, temperatures, gas and fluid compositions and thermal transfers. Such sectioned capsules can provide additional environmental monitoring and can be built of lined and engineered tailings berms similar to the primary exterior walls. In one embodiment, sections within the impoundment 100 can be used to place materials in isolation, in the absence of external heat, or with the intent of limited or controlled combustion or solvent application. Lower content hydrocarbon bearing material can be useful as a combustion material or as fill or a berm wall building material. Material which does not meet a various cut-off grade thresholds can also be sequestered without alteration in an impoundment dedicated for such purpose. In such embodiments, such areas may be completely isolated or bypassed by heat, solvents, gases, liquids, or the like. Optional monitoring devices and/or equipment can be permanently or temporarily installed within the impoundment or outside perimeters of the impoundments in order to verify containment of the sequestered material.\|[0076] Walls 102 and 104 as well as cap 116 and impermeable layer 112 can be engineered and reinforced by gabions 146 and or geogrid 148 layered in fill compaction. Alternatively, these walls 102, 104, 116 and 112 which comprise the permeability control impoundment and collectively define the encapsulated volume can be formed of any other suitable material as previously described. In this embodiment, the impoundment 100 includes side walls 102 and 104 which are self-supporting. In one embodiment, tailings berms, walls, and floors can be compacted and engineered for structure as well as permeability. The use of compacted geogrids and other deadman structures for support of berms and embankments can be included prior to or incorporated with permeability control layers which may include sand, clay, bentonite clay, gravel, cement, grout, reinforced cement, refractory cements, insulations, geo-membranes, drainpipes, temperature resistant insulations of penetrating heated pipes, etc.\|[0077] In one alternative embodiment, the permeability control impoundment can include side walls which are compacted earth and/or undisturbed geological formations while the cap and floors are impermeable. Specifically, in such embodiments an impermeable cap can be used to prevent uncontrolled escape of volatiles and gases from the impoundment such that appropriate gas collection outlets can be used. Similarly, an impermeable floor can be used to contain and direct collected liquids to a suitable outlet such the drain system 133 to remove liquid products from lower regions of the impoundment. Although impermeable side walls can be desirable in some embodiments, such are not always required. In some cases, side walls can be exposed undisturbed earth or compacted fill or earth, or other permeable material. Having permeable side walls may allow some small egress of gases and/or liquids from the impoundment.\|[0078] Although not shown, above, below, around and adjacent to constructed capsule containment vessels environmental hydrology measures can be engineered to redirect surface water away from the capsule walls, floors, caps, etc. during operation. Further, gravity assisted drainage pipes and mechanisms can be utilized to aggregate and channel fluids, liquids or solvents within the encapsulated volume to central gathering, pumping, condensing, heating, staging and discharge pipes, silos, tanks, and/or wells as needed. In a similar manner, steam and/or water which is intentionally introduce, e.g. for tar sands bitumen treatment, can be recycled.\|[0079] Once wall structures 102 and 104 have been constructed above a constructed and impermeable floor layer 112 which commences from ground surface 106, the mined rubble 120 (which may be crushed or classified according to size or hydrocarbon richness), can be placed in layers upon (or next to) placed tubular heating pipes 118, fluid drainage pipes 124, and, or gas gathering or injection pipes 126. These pipes can be oriented and designed in any optimal flow pattern, angle, length, size, volume, intersection, grid, wall sizing, alloy construction, perforation design, injection rate, and extraction rate. In some cases, pipes such as those used for heat transfer can be connected to, recycled through or derive heat from heat source 134. Alternatively, or in combination with, recovered gases can be condensed by a condenser 140. Heat recovered by the condenser can be optionally used to supplement heating of the permeable body or for other process needs.\|[0080] Heat source 134 can derive, amplify, gather, create, combine, separate, transmit or include heat derived from any suitable heat source including, but not limited to, fuel cells (e.g. solid oxide fuel cells, molten carbonate fuel cells and the like), solar sources, wind sources, hydrocarbon liquid or gas combustion heaters, geothermal heat sources, nuclear power plant, coal fired power plant, radio frequency generated heat, wave energy, flameless combustors, natural distributed combustors, or any combination thereof. In some cases, electrical resistive heaters or other heaters can be used, although fuel cells and combustion-based heaters are particularly effective. In some locations, geothermal water can be circulated to the surface in adequate amounts to heat the permeable body and directed into the infrastructure.\|[0081] In another embodiment, electrically conductive material can be distributed throughout the permeable body and an electric current can be passed through the conductive material sufficient to generate heat. The electrically conductive material can include, but is not limited to, metal pieces or beads, conductive cement, metal coated particles, metal-ceramic composites, conductive semi-metal carbides, calcined petroleum coke, laid wire, combinations of these materials, and the like. The electrically conductive material can be premixed having various mesh sizes or the materials can be introduced into the permeable body subsequent to formation of the permeable body.\|[0082] Liquids or gases can transfer heat from heat source 134, or in another embodiment, in the cases of hydrocarbon liquid or gas combustion, radio frequency generators (microwaves), or fuel cells all can, but need not, actually generate heat inside of capsule impoundment area 114 or 122. In one embodiment, heating of the permeable body can be accomplished by convective heating from hydrocarbon combustion. Of particular interest is hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen. Stoichiometric conditions can allow for significantly increased heat gas temperatures. Stoichiometric combustion can employ but does not generally require a pure oxygen source which can be provided by known technologies including, but not limited to, oxygen concentrators, membranes, electrolysis, and the like. In some embodiments oxygen can be provided from air with stoichiometric amounts of oxygen and hydrogen. Combustion off gas can be directed to an ultra-high temperature heat exchanger, e.g. a ceramic or other suitable material having an operating temperature above about 2500° F. Air obtained from ambient or recycled from other processes can be heated via the ultra high temperature heat exchanger and then sent to the impoundment for heating of the permeable body. The combustion off gases can then be sequestered without the need for further separation, i.e. because the off gas is predominantly carbon dioxide and water.\|[0083] In order to minimize heat losses, distances can be minimized between the combustion chamber, heat exchanger, and impoundments. Therefore, in one specific detailed embodiment portable combustors can be attached to individual heating conduits or smaller sections of conduits. Portable combustors or burners can individually provide from about 100,000 Btu to about 1,000,000 Btu with about 600,000 Btu per pipe generally being sufficient.\|[0084] Alternatively, in-capsule combustion can be initiated inside of isolated capsules within a primary constructed capsule containment structure. This process partially combusts hydrocarbonaceous material to provide heat and intrinsic pyrolysis. Unwanted air emissions 144 can be captured and sequestered in a formation 108 once derived from capsule containment 114, 122 or from heat source 134 and delivered by a drilled well bore 142. Heat source 134 can also create electricity and transmit, transform or power via electrical transmission lines 150. The liquids or gases extracted from capsule impoundment treatment area 114 or 122 can be stored in a nearby holding tank 136 or within a capsule containment 114 or 122. For example, the impermeable floor layer 112 can include a sloped area 110 which directs liquids towards drain system 133 where liquids are directed to the holding tank.\|[0085] As rubble material 120 is placed with piping 118, 124, 126, and 128, various measurement devices or sensors 130 are envisioned to monitor temperature, pressure, fluids, gases, compositions, heating rates, density, and all other process attributes during the extractive process within, around, or underneath the engineered capsule containment impoundment 100. Such monitoring devices and sensors 130 can be distributed anywhere within, around, part of, connected to, or on top of placed piping 118, 124, 126, and 128 or, on top of, covered by, or buried within rubble material 120 or impermeable barrier zone 112.\|[0086] As placed rubble material 120 fills the capsule treatment area 114 or 122, 120 becomes the ceiling support for engineered impermeable cap barrier zone 138, and wall barrier construction 170, which may include any combination of impermeability and engineered fluid and gas barrier or constructed capsule construction comprising those which may make up 112 including, but not limited to clay 162, compacted fill or import material 164, cement or refractory cement containing material 166, geo synthetic membrane, liner or insulation 168. Above 138, fill material which can be oriented as ceiling cap 116 is placed to create lithostatic pressure upon the capsule treatment areas 114 or 122. Covering the permeable body with compacted fill sufficient to create an increased lithostatic pressure within the permeable body can be useful in further increasing hydrocarbon product quality. A compacted fill ceiling can substantially cover the permeable body, while the permeable body in return can substantially support the compacted fill ceiling. The compacted fill ceiling can further be sufficiently impermeable to removed hydrocarbon or an additional layer of permeability control material can be added in a similar manner as side and/or floor walls. Additional pressure can be introduced into extraction capsule treatment area 114 or 122 by increasing any gas or fluid once extracted, treated or recycled, as the case may be, via any of piping 118, 124, 126, or 128. All relative measurements, optimization rates, injection rates, extraction rates, temperatures, heating rates, flow rates, pressure rates, capacity indicators, chemical compositions, or other data relative to the process of heating, extraction, stabilization, sequestration, impoundment, upgrading, refining or structure analysis within the capsule impoundment 100 are envisioned through connection to a computing device 132 which operates computer software for the management, calculation and optimization of the entire process. Further, core drilling, geological reserve analysis and assay modeling of a formation prior to blasting, mining and hauling (or at any time before, after or during such tasks) can serve as data input feeds into computer controlled mechanisms that operate software to identify optimal placements, dimensions, volumes and designs calibrated and cross referenced to desired production rate, pressure, temperature, heat input rates, gas weight percentages, gas injection compositions, heat capacity, permeability, porosity, chemical and mineral composition, compaction, density. Such analysis and determinations may include other factors like weather data factors such as temperature and air moisture content impacting the overall performance of the constructed infrastructure. Other data such as ore moisture content, hydrocarbon richness, weight, mesh size, and mineral and geological composition can be utilized as inputs including time value of money data sets yielding project cash flows, debt service, and internal rates of return.\|[0087] FIG. 2A shows a collection of impoundments including an uncovered or uncapped capsule impoundment 100, containing sectioned capsule impoundments 122 inside of a mining quarry 200 with various elevations of bench mining. FIG. 2B illustrates a single impoundment 122 without associated conduits and other aspects merely for clarity. This impoundment can be similar to that illustrated in FIG. 1 or any other configuration. In some embodiments, it is envisioned that mining rubble can be transferred down chutes 230 or via conveyors 232 to the quarry capsule impoundments 100 and 122 without any need of mining haul trucks.\|[0088] FIG. 3 shows the engineered permeability barriers 112 below capsule impoundment 100 resting on existing grade 106 of formation 108 with cap covering material or fill 302 on the sides and top of capsule impoundment 100 to ultimately (following the process) cover and reclaim a new earth surface 300. Indigenous plants which may have been temporarily moved from the area may be replanted such as trees 306. The constructed infrastructures can generally be single use structures which can be readily and securely shut down with minimal additional remediation. This can dramatically reduce costs associated with moving large volumes of spent materials. However, in some circumstances the constructed infrastructures can be excavated and reused. Some equipment such as radio frequency (RF) mechanisms, tubulars, devices, and emitters may be recovered from within the constructed impoundment upon completion of hydrocarbon recovery.\|[0089] FIG. 4 shows computer means 130 controlling various property inputs and outputs of conduits 118, 126, or 128 connected to heat source 134 during the process among the subdivided impoundments 122 within a collective impoundment 100 to control heating of the permeable body. Similarly, liquid and vapor collected from the impoundments can be monitored and collected in tank 136 and condenser 140, respectively. Condensed liquids from the condenser can be collected in tank 141, while non-condensable vapor collected at unit 143. As described previously, the liquid and vapor products can be combined or more often left as separate products depending on condensability, target product, and the like. A portion of the vapor product can be optionally condensed and combined with the liquid products in tank 136. However, much of the vapor product will be C4 and lighter gases which can be burned, sold, or used within the process. For example, hydrogen gas may be recovered using conventional gas separation and used to hydrotreat the liquid products according to conventional upgrading methods, e.g. catalytic, etc. or the non-condensable gaseous product can be burned to produce heat for use in heating the permeable body, heating an adjacent or nearby impoundment, heating service or personnel areas, or satisfying other process heat requirements. The constructed infrastructure can include thermocouples, pressure meters, flow meters, fluid dispersion sensors, richness sensors and any other conventional process control devices distributed throughout the constructed infrastructure. These devices can be each operatively associated with a computer such that heating rates, product flow rates, and pressures can be monitored or altered during heating of the permeable body. Optionally, in-place agitation can be performed using, for example, ultrasonic generators which are associated with the permeable body. Such agitation can facilitate separation and pyrolysis of hydrocarbons from the underlying solid materials with which they are associated. Further, sufficient agitation can reduce clogging and agglomeration throughout the permeable body and the conduits.\|[0090] FIG. 5 shows how any of the conduits can be used to transfer heat in any form of gas, liquid or heat via transfer means 510 from any sectioned capsule impoundment to another. Then, cooled fluid can be conveyed via heat transfer means 512 to the heat originating capsule 500, or heat originating source 134 to pick up more heat from capsule 500 to be again recirculated to a destination capsule 522. Thus, various conduits can be used to transfer heat from one impoundment to another in order to recycle heat and manage energy usage to minimize energy losses.\|[0091] In yet another aspect, a hydrogen donor agent can be introduced into the permeable body during the step of heating. The hydrogen donor agent can be any composition which is capable of hydrogenation of the hydrocarbons and can optionally be a reducing agent. Non-limiting examples of suitable hydrogen donor agents can include synthesis gas, propane, methane, hydrogen, natural gas, natural gas condensate, industrial solvents such as acetones, toluenes, benzenes, xylenes, cumenes, cyclopentanes, cyclohexanes, lower alkenes (C4-C10), terpenes, substituted compounds of these solvents, etc., and the like. Further, the recovered hydrocarbons can be subjected to hydrotreating either within the permeable body or subsequent to collection. Advantageously, hydrogen recovered from the gas products can be reintroduced into the liquid product for upgrading. Regardless, hydrotreating or hydrodesulfurization can be very useful in reducing nitrogen and sulfur content in final hydrocarbon products. Optionally, catalysts can be introduced to facilitate such reactions. In addition, introduction of light hydrocarbons into the permeable body can result in reforming reactions which reduce the molecular weight, while increasing the hydrogen to carbon ratio. This is particularly advantageous due at least in part to high permeability of the permeable body, e.g. often around 30%-40% void volume although void volume can generally vary from about 10% to about 50% void volume. Light hydrocarbons which can be injected can be any which provide reforming to recovered hydrocarbons. Non-limiting examples of suitable light hydrocarbons include natural gas, natural gas condensates, industrial solvents, hydrogen donor agents, and other hydrocarbons having ten or fewer carbons, and often five or fewer carbons. Currently, natural gas is an effective, convenient, and plentiful light hydrocarbon. As mentioned previously, various solvents or other additives can also be added to aid in extraction of hydrocarbon products from the oil shale and can often also increase fluidity.\|[0092] The light hydrocarbon can be introduced into the permeable body by conveying the same through a delivery conduit having an open end in fluid communication with a lower portion of the permeable body such that the light hydrocarbons (which are a gas under normal operating conditions) permeate up through the permeable body. Alternatively, this same approach can be applied to recovered hydrocarbons which are first delivered to an empty impoundment. In this way, the impoundment can act as a holding tank for direct products from a nearby impoundment and as a reformer or upgrader. In this embodiment, the impoundment can be at least partially filled with a liquid product where the gaseous light hydrocarbon is passed through and allowed to contact the liquid hydrocarbon products at temperatures and conditions sufficient to achieve reforming in accordance with well known processes. Optional reforming catalysts which include metals such as Pd, Ni or other suitable catalytically active metals can also be included in the liquid product within the impoundment. The addition of catalysts can serve to lower and/or adjust reforming temperature and/or pressure for particular liquid products. Further, the impoundments can be readily formed at almost any depth. Thus, optimal reforming pressures (or recovery pressures when using impoundment depth as pressure control measure for recovery from a permeable body) can be designed based on hydrostatic pressure due to the amount of liquid in the impoundment and the height of the impoundment, i.e. P=ρgh. In addition, the pressure can vary considerably over the height of the impoundment sufficient to provide multiple reforming zones and tailorable pressures. Generally, pressures within the permeable body can be sufficient to achieve substantially only liquid extraction, although some minor volumes of vapor may be produced depending on the particular composition of the permeable body. As a general guideline, pressures can range from about 5 atm to about 50 atm, although pressures from about 6 atm to about 20 atm can be particularly useful. However, any pressure greater than about atmospheric can be used.\|[0093] In one embodiment, extracted crude has fines precipitated out within the subdivided capsules. Extracted fluids and gases can be treated for the removal of fines and dust particles. Separation of fines from shale oil can be accomplished by techniques such as, but not limited to, hot gas filtering, precipitation, and heavy oil recycling.\|[0094] Hydrocarbon products recovered from the permeable body can be further processed (e.g. refined) or used as produced. Any condensable gaseous products can be condensed by cooling and collection, while non-condensable gases can be collected, burned as fuel, reinjected, or otherwise utilized or disposed of. Optionally, mobile equipment can be used to collect gases. These units can be readily oriented proximate to the control infrastructure and the gaseous product directed thereto via suitable conduits from an upper region of the control infrastructure.\|[0095] In yet another alternative embodiment, heat within the permeable body can be recovered subsequent to primary recovery of hydrocarbon materials therefrom. For example, a large amount of heat is retained in the permeable body. In one optional embodiment, the permeable body can be flooded with a heat transfer fluid such as water to form a heated fluid, e.g. heated water and/or steam. At the same time, this process can facilitate removal of some residual hydrocarbon products via a physical rinsing of the spent shale solids. In some cases, the introduction of water and presence of steam can result in water gas shift reactions and formation of synthesis gas. Steam recovered from this process can be used to drive a generator, directed to another nearby infrastructure, or otherwise used. Hydrocarbons and/or synthesis gas can be separated from the steam or heated fluid by conventional methods.\|[0096] Although the methods and infrastructure allow for improved permeability and control of operating conditions, significant quantities of unrecovered hydrocarbons, precious metals, minerals, sodium bicarbonate or other commercially valuable materials often remain in the permeable body. Therefore, a selective solvent can be injected or introduced into the permeable body. Typically, this can be done subsequent to collecting the hydrocarbons, although certain selective solvents can be beneficially used prior to heating and/or collection. This can be done using one or more of the existing conduits or by direct injection and percolation through the permeable body. The selective solvent or leachate can be chosen as a solvent for one or more target materials, e.g. minerals, precious metal, heavy metals, hydrocarbons, or sodium bicarbonate. In one specific embodiment, steam or carbon dioxide can be used as a rinse of the permeable body to dislodge at least a portion of any remaining hydrocarbons. This can be beneficial not only in removing potentially valuable secondary products, but also in cleaning remaining spent materials of trace heavy metal or inorganics to below detectable levels in order to comply with regulatory standards or to prevent inadvertent leaching of materials at a future date.\|[0097] More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body. Typically, such recovery of materials can be performed prior to heat treatment of the permeable body. Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like. For example, heavy metals, bauxite or aluminum, and mercury can be removed by flooding the permeable body with an appropriate solvent and recirculating the resulting leachate through appropriately designed ion exchange resins (e.g. beads, membranes, etc.).\|[0098] Similarly, bioextraction, bioleaching, biorecovery, or bioremediation of hydrocarbon material, spent materials, or precious metals can be performed to further improve remediation, extract valuable metals, and restoration of spent material to environmentally acceptable standards. In such bioextraction scenarios, conduits can be used to inject catalyzing gases as a precursor which helps to encourage bioreaction and growth. Such microorganisms and enzymes can biochemically oxidize the ore body or material or cellulosic or other biomass material prior to an ore solvent extraction via bio-oxidation. For example, a perforated pipe or other mechanism can be used to inject a light hydrocarbon (e.g. methane, ethane, propane or butane) into the permeable body sufficient to stimulate growth and action of native bacteria. Bacteria can be native or introduced and may grow under aerobic or anaerobic conditions. Such bacteria can release metals from the permeable body which can then be recovered via flushing with a suitable solvent or other suitable recovery methods. The recovered metals can then be precipitated out using conventional methods.\|[0099] Synthesis gas can also be recovered from the permeable body during the step of heating. Various stages of gas production can be manipulated through processes which raise or lower operating temperatures within the encapsulated volume and adjust other inputs into the impoundment to produce synthetic gases which can include but are not limited to, carbon monoxide, hydrogen, hydrogen sulfide, hydrocarbons, ammonia, water, nitrogen or various combinations thereof. In one embodiment, temperature and pressure can be controlled within the permeable body to lower CO2 emissions as synthetic gases are extracted.\|[0100] Hydrocarbon product recovered from the constructed infrastructures can most often be further processed, e.g. by upgrading, refining, etc. Sulfur from related upgrading and refining processing can be isolated in various constructed sulfur capsules within the greater structured impoundment capsule. Constructed sulfur capsules can be spent constructed infrastructures or dedicated for the purpose of storage and isolation after desulfurization.\|[0101] Similarly, spent hydrocarbonaceous material remaining in the constructed infrastructure can be utilized in the production of cement and aggregate products for use in construction or stabilization of the infrastructure itself or in the formation of offsite constructed infrastructures. Such cement products made with the spent shale may include, but are not limited to, mixtures with Portland cement, calcium salt, volcanic ash, perlite, synthetic nano carbons, sand, fiber glass, crushed glass, asphalt, tar, binding resins, cellulosic plant fibers, and the like.\|[0102] In still another embodiment, injection, monitoring and production conduits or extraction egresses can be incorporated into any pattern or placement within the constructed infrastructure. Monitoring wells and constructed geo membrane layers beneath or outside of the constructed capsule containment can be employed to monitor unwanted fluid and moisture migration outside of containment boundaries and the constructed infrastructure.\|[0103] Although a filled and prepared constructed infrastructure can often be immediately heated to recover hydrocarbons, this is not required. For example, a constructed infrastructure which is built and filled with mined hydrocarbonaceous material can be left in place as a proven reserve. Such structures are less susceptible to explosion or damage due to terrorist activity and can also provide strategic reserves of unprocessed petroleum products, with classified and known properties so that economic valuations can be increased and more predictable. Long term petroleum storage often faces quality deterioration issues over time. Thus, these approaches can optionally be used for long term quality insurance and storage with reduced concerns regarding breakdown and degradation of hydrocarbon products.\|[0104] In still another aspect, the high quality liquid product can be blended with more viscous lower quality (e.g. lower API) hydrocarbon products. For example, kerogen oil produced from the impoundments can be blended with bitumen to form a blended oil. The bitumen is typically not transportable through an extended pipeline under conventional and accepted pipeline standards and can have a viscosity substantially above and an API substantially below that of the kerogen oil. By blending the kerogen oil and bitumen, the blended oil can be rendered transportable without the use of additional diluents or other viscosity or API modifiers. As a result, the blended oil can be pumped through a pipeline without requiring additional treatments to remove a diluent or returning such diluents via a secondary pipeline. Conventionally, bitumen is combined with a diluent such as natural gas condensate or other low molecular weight liquids, to allow pumping to a remote location. The diluent is removed and returned via a second pipeline back to the bitumen source. These approaches allow for elimination of returning diluent and simultaneous upgrading of the bitumen.\|[0105] Difficult problems can thus be solved related to the extraction of hydrocarbon liquids and gases from surface or underground mined hydrocarbon bearing deposits such as oil shale, tar sands, lignite, and coal, and from harvested biomass. Among other things, these methods and systems help reduce cost, increase volume output, lower air emissions, limit water consumption, prevent underground aquifer contamination, reclaim surface disturbances, reduce material handling costs, remove dirty fine particulates, and improve composition of recovered hydrocarbon liquid or gas. Water contamination issues can also be addressed with a safer, more predictable, engineered, observable, repairable, adaptable and preventable water protection structure.\|[0106] Although the described methods and systems are mining-dependent, they are not limited or encumbered to conventional aboveground (ex-situ) retorting processes. This approach improves upon the benefits of surface retorts including better process control of temperature, pressure, injection rates, fluid and gas compositions, product quality and better permeability due to processing and heating mined rubble. These advantages are available while still addressing the volume, handling, and scalability issues most fabricated surface retorts cannot provide.\|[0107] Other improvements which can be realized are related to environmental protection. Conventional surface retorts have had the problem of spent shale after it has been mined and has passed through a surface retort. Spent shale which has been thermally altered requires special handling to reclaim and isolate from surface drainage basins and underground aquifers. These methods and systems can address reclamation and retorting in a uniquely combined approach. In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants.\|[0108] It is to be understood that the above-referenced arrangements are illustrative of the application for the principles of the present invention. Thus, while the present invention has been described above in connection with the exemplary embodiments, it will be apparent to those of ordinary skill in the art that numerous modifications and alternative arrangements can be made without departing from the principles and concepts of the invention as set forth in the claims.	Family Number\|(35298)\|35298\|Title\|(AU2010213862 B2)\|Carbon management and sequestration from encapsulated control infrastructures\|(AU2010213862 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(CA2752524 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(CN102395657 A)\|Carbon management and sequestration from encapsulated control infrastructures \|(EA201171023 A1)\|Carbon monitoring and sequestration from sealed controlled infrastructures\|(EP2406353 A4)\|Carbon management and sequestration from encapsulated control infrastructures\|(EP2406353 A2)\|Carbon management and sequestration from encapsulated control infrastructures\|(IL-214555 A)\|Carbon management and sequestration from encapsulated control infrastructures\|(MA--33117 B1)\|Carbon management and sequestration from encapsulated control infrastructures\|(MX2011008525 A)\|Carbon management and sequestration from encapsulated control infrastructures\|Carbon management and sequestration from encapsulated control infrastructures.\|(MX-319678 B)\|Carbon management and sequestration from encapsulated control infrastructure.\|(US8323481 B2)\|Carbon management and sequestration from encapsulated control infrastructures\|(US20100200465 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(WO201093684 A3)\|Carbon management and sequestration from encapsulated control infrastructures\|(WO201093684 A2)\|Carbon management and sequestration from encapsulated control infrastructures\|(IN2011MN01897 A)\|Carbon management and sequestration from encapsulated control infrastructures\|(EG--26451 A)\|Carbon management and sequestration from encapsulated control infrastructures\|(MY-152266 A)\|Carbon management and sequestration form encapsulated control infrastructures\|(TN2011000396 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(BR201008447 A2)\|Carbon management and sequestration from encapsulated control infrastructures\|(ZA201106558 B)\|Carbon management and sequestration from encapsulated control infrastructures\|(PE201200704 A1)\|Carbon management and sequestration from encapsulated control infrastructures\|(AP2011005878 A0)\|Carbon management and sequestration from encapsulated control infrastructures\|Carbon management and sequestration from encapsulated control infrastructures.\|(GE201406167 B)\|Carbon management and sequestration from encapsulated control infrastructures\|(VE2010000234 A)\|Carbon management and sequestration from encapsulated control infrastructure.\|Advantages / Prev. Drawbacks\|(CN102395657 A)\|Other methods include in situ radio frequency methods ( microwaves ) and " modified " in situ processes where underground mining , blasting and retorting have been used in combination to produce crushed rock from a formation to allow for better heat transfer and product removal . \|	Basic materials chemistry\|Civil 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KR100595792; KR10-0595792\|\|JP2000317302; CN101125651; CN1956768; US20080190815; KR100595792\|\|\|\|\|\|\|US4133580; US4423907; US4424021; US4717146; US4984594; US6841077; US6991033; US20070000662; US20090000744; US7862705; US7862706; US4430195; US5868202; US6854929; US7004247; US7004251; US7004678; US20070023186; US3652447; US4502920; US5190405; US5193934; US4017119; US4151068; US4440446; US6051137; US6543535; US6543539; US6875356; US6881009; US7032660; US3661423; US3954140; US4155967; US4266612; US4266826; US4449586; US5114497; US6732796; US7040397; US7040399; US7048051; US7051811; US7534926; US4029571; US4096912; US4158622; US4452689; US4454915; US5024487; US5221827; US5318116; US6902138; US7066254; US20110138649; US1919636; US4851134; US5229583; US6419423; US6918443; US7070758; US7073578; US7077198; US7077199; US4043595; US4106814; US4219237; US5041209; US5137539; US5340467; US5543041; US5656239; US5660500; US6102622; US6110359; US6923257; US6929330; US7090013; US7091460; US20080190813; US20080190816; US20080190818; US20080192815; US20100200467; US2481051; US4221648; US5244310; US5553189; US5948253; US20060213657; US3910834; US4294563; US4353418; US5674424; US6632047; US20040211569; US6951247; US3919390; US4199327; US5139535; US1919636; US2481051; US3617471; US3652447; US3661423; US3910834; US3954140; US4017119; US4029571; US4043595; US4096912; US4106814; US4133580; US4151068; US4155967; US4158622; US4171146; US4219237; US4221648; US4234230; US4241952; US4266612; US4266826; US4294563; US4303533; US4353418; US4376107; US4415365; US4423907; US4424021; US4430195; US4440446; US4449586; US4452689; US4454915; US4502920; US4851134; US4879019; US4984594; US5024487; US5041209; US5076727; US5114497; US5137539; US5190405; US5193934; US5221827; US5229583; US5244310; US5271693; US5318116; US5340467; US5372621; US5372708; US5478443; US5543041; US5553189; US5656239; US5660500; US5674424; US5843214; US5868202; US5948253; US5997214; US6051137; US6102622; US6110359; US6419423; US6485232; US6543535; US6543539; US6632047; US6732796; US6811683; US6824328; US6841077; US6854929; US6875356; US6881009; US6902138; US6918443; US6923257; US6929330; US6951247; US6962466; US6991033; US7004247; US7004251; US7004678; US7032660; US7040397; US7040399; US7048051; US7051811; US7066254; US7070758; US7073578; US7077198; US7077199; US7090013; US7091460; US7114566; US7121342; US7534926; US7862705; US7862706; KR10-0595792; JP2005306721; JP2009090168; US20040211569; US20060213657; US20070000662; US20070023186; US20080077430; US20080190813; US20080190815; US20080190816; US20080190818; US20090007484; US20090250380; US20100200467; US20110138649	(EP2406353)\|Search Report references [Examiner]\|-See also references of WO 2010093684A2\|\|(US8323481)\|Applicant references\|-U.S. Appl. No. 12/703,560, filed Feb. 10, 2010; Todd Dana; Office action issued Nov. 18, 2011.\|-U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana; notice of allowance issued Oct. 26, 2011.\|-Alternative Methods for Fluid Delivery and Recovery; Manual; Sep. 1994; United States Environmental Protection Agency; 87 pgs.\|-U.S. Appl. No. 12/703,638, filed Feb. 10, 2010, Todd Dana.\|-U.S. Appl. No. 12/704,440, filed Feb. 11, 2010, Todd Dana.\|-U.S. Appl. No. 12/702,899, filed Feb. 9, 2010, Todd Dana.\|-U.S. Appl. No. 12/703,560, filed Feb. 10, 2010, Todd Dana.\|-U.S. Appl. No. 12/704,596, filed Feb. 12, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,073, filed Feb. 5, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,141, filed Feb. 5, 2010, Todd Dana.\|-PCT Application PCT/US2010/058948; filed Dec. 3, 2010; James W. Patten; International Search Report mailed Aug. 31, 2011.\|-PCT Application PCT/US2010/060854; filed Dec. 16, 2010; James W. Patten; International Search Report mailed Aug. 26, 2011.\|-Slow Sand Filter: http://en.wikipedia.org/wiki/Slow-sand-filter; Nov. 9, 2009; 4 pages.\|-Sand Filter: http://en.wikipedia.org/wiki/Sand-filter; Nov. 9, 2009; 6 pages.\|-RELATED CASE: U.S. Appl. No. 12/960,215, filed Dec. 3, 2010; James Patten.\|-RELATED CASE: U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana.\|-U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana; office action issued Jun. 1, 2011.\|-PCT Application PCT/US2010/023740; filed Feb. 10, 2010; Todd Dana; ISR issued Sep. 16, 2010.\|-U.S. Appl. No. 12/703,560, filed Feb. 10, 2010; Todd Dana; office action issued Apr. 24, 2012.\|-U.S. Appl. No. 12/703,560, filed Feb. 10, 2010; Todd Dana; notice of allowance dated Sep. 4, 2012.\|\|(WO2010/093684)\|International Search Report [Examiner]\|-See also references of EP 2406353A2\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|	GRANTED	(EP2406353)\|LAPSED\|(US8323481)\|LAPSED\|(WO2010/093684)\|LAPSED\|(CN102395657)\|LAPSED\|(GEP20146167)\|GRANTED\|(MY152266)\|GRANTED\|(MX319678)\|GRANTED\|(UA104616)\|GRANTED\|(EG26451)\|GRANTED\|(AU2010213862)\|EXPIRED\|(ZA201106558)\|GRANTED\|(MA33117)\|GRANTED\|(BRPI1008447)\|LAPSED\|(TN2011000396)\|PENDING\|(VE2010000234)\|LAPSED\|(PE20120704)\|REVOKED\|(EA201171023)\|LAPSED\|(IN1897/MUMNP/2011)\|LAPSED\|(AP2011005878)\|LAPSED\|(IL214555)\|LAPSED\|(CA2752524)\|LAPSED	ALIVE	(EP2406353)\|DEAD\|(US8323481)\|DEAD\|(WO2010/093684)\|DEAD\|(CN102395657)\|DEAD\|(GEP20146167)\|ALIVE\|(MY152266)\|ALIVE\|(MX319678)\|ALIVE\|(UA104616)\|ALIVE\|(EG26451)\|ALIVE\|(AU2010213862)\|DEAD\|(ZA201106558)\|ALIVE\|(MA33117)\|ALIVE\|(BRPI1008447)\|DEAD\|(TN2011000396)\|ALIVE\|(VE2010000234)\|DEAD\|(PE20120704)\|DEAD\|(EA201171023)\|DEAD\|(IN1897/MUMNP/2011)\|DEAD\|(AP2011005878)\|DEAD\|(IL214555)\|DEAD\|(CA2752524)\|DEAD	(EP2406353)\|LEGAL DETAILS FOR EP2406353\|Actual or expected expiration date=2015-03-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP10741655\|Application date=2010-02-10\|Standardized application number=2010EP-0741655\|Event publication date=2011-12-16\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2012-01-18\|Event code=EP/A2\|Event group=Examination events\|Application published without search report\|Publication country=EP\|Publication number=EP2406353\|Publication stage code=A2\|Publication date=2012-01-18\|Standardized publication number=EP2406353\|Event publication date=2012-01-18\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2011-09-12\|Event publication date=2012-01-18\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR\|Event publication date=2012-05-16\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2014-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP2406353\|Publication stage code=A4\|Publication date=2014-09-17\|Standardized publication number=EP2406353\|Event publication date=2014-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2014-08-21\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2015-09-18\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2015-10-21\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2015-03-20\|(US8323481)\|LEGAL DETAILS FOR US8323481\|Actual or expected expiration date=2025-01-06\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-05\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US12701156\|Application date=2010-02-05\|Standardized application number=2010US-12701156\|Event publication date=2010-02-05\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:MCCAIG, BRIAN A\|Event publication date=2010-02-05\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1774\|Event publication date=2010-02-05\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 2488-025.NP\|Event publication date=2010-02-05\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 20551\|Event publication date=2010-02-05\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2010-02-05\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2010-02-26\|Event code=US/INCD\|Event group=Examination events OAO\|Notice Mailed--Application Incomplete--Filing Date Assigned\|Event publication date=2010-02-26\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2010-03-11\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DANA, TODD;PATTEN, JAMES W.;SIGNING DATES FROM 20090511 TO 20090623\|Reel/frame:024064/0164\|OWNER:RED LEAF RESOURCES, INC., UTAH\|Event publication date=2010-03-17\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|SECURITY AGREEMENT\|Assignors:RED LEAF RESOURCES, INC., DBA ECOSHALE AND ECOSHALE ENERGY;RED LEAF HOLDINGS, LLC;NATIONS MINING, LLC;AND OTHERS\|Reel/frame:024097/0397\|OWNER:CARDINAL ENERGY HOLDINGS, LLC, UTAH\|Effective date of the event=2009-07-02\|Event publication date=2010-04-12\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DANA, TODD;PATTEN, JAMES W.;SIGNING DATES FROM 20100317 TO 20100324\|Reel/frame:024215/0959\|OWNER:RED LEAF RESOURCES, INC., UTAH\|Event publication date=2010-04-26\|Event code=US/FLFEE\|Event group=Payment or non-payment notifications\|Payment of additional filing fee/Preexam\|Event publication date=2010-05-06\|Event code=US/POAC\|Event group=Change of name or address\|Change in Power of Attorney (May Include Associate POA)\|Event publication date=2010-05-06\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2010-05-10\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|RELEASE BY SECURED PARTY\|Assignor:CARDINAL ENERGY HOLDINGS, LLC.\|Reel/frame:024357/0626\|OWNER:RED LEAF RESOURCES, INC., D/B/A ECOSHALE, ECHOSHAL\|Effective date of the event=2010-05-07\|Event publication date=2010-05-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2010-08-12\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20100200465\|Publication stage code=A1\|Publication date=2010-08-12\|Standardized publication number=US20100200465\|Event publication date=2010-08-12\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2011-01-15\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-01-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-05-23\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-06-28\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-10-28\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-11-21\|Event code=US/RESTREQ\|Event group=Examination events Corrections OAO\|Restriction/Election Requirement\|Event publication date=2011-12-14\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-01-03\|Event code=US/ELC\|Event group=Examination events OAI\|Response to Election / Restriction Filed\|Event publication date=2012-03-07\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2012-03-12\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2012-03-12\|R4R=103a\|RJST=non-final\|Rejected claims 1 and 11-13; 1 and 11-12\|RJCT=US5139535\|RJCT=US4199327\|Event publication date=2012-06-11\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2012-07-23\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-07-25\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2012-07-29\|Event code=US/ZAAA\|Event group=Administrative notifications Payment or non-payment notifications\|NOTICE OF ALLOWANCE AND FEES DUE\|Original code: NOA\|Event publication date=2012-07-30\|Event code=US/ZAAB\|Event group=Administrative notifications Examination events\|NOTICE OF ALLOWANCE MAILED\|Original code: MN/=.\|Event publication date=2012-07-30\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2012-09-20\|Event code=US/M327\|Event group=Examination events OAO\|Miscellaneous Communication to Applicant - No Action Count\|Event publication date=2012-10-12\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-10-19\|Event code=US/M327\|Event group=Examination events OAO\|Miscellaneous Communication to Applicant - No Action Count\|Event publication date=2012-10-30\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2012-10-30\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2012-11-02\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2012-11-14\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2012-12-04\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US08323481\|Publication stage code=B2\|Publication date=2012-12-04\|Standardized publication number=US8323481\|Event publication date=2012-12-04\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 240 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 71 Adjustment total: \|Number of days of extension=169\|Event publication date=2015-12-15\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2016-05-16\|Event code=US/FPAY\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Fee payment recorded\|Annual fees payment date=2016-05-16\|Year of payment of annual fees=4\|Event publication date=2019-12-17\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|Event publication date=2020-04-07\|Event code=US/MAFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|Maintenance Fee Payment\|Annual fees payment date=2020-04-07\|Year of payment of annual fees=8\|PAYMENT OF MAINTENANCE FEE, 8TH YR, SMALL ENTITY (ORIGINAL EVENT CODE: M2552)\|Entity status of patent owner: SMALL ENTITY\|Event publication date=2020-04-07\|Event code=US/M2552\|Event group=Payment or non-payment notifications\|Payment of Maintenance Fee, 8th Yr, Small Entity\|Event publication date=2023-12-19\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=11\|Event publication date=2024-07-22\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2024-12-04\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2024-12-04\|Event publication date=2025-01-06\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2025-01-06\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|(WO2010/093684)\|LEGAL DETAILS FOR WO2010/093684\|Actual or expected expiration date=2012-08-12\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2010023740\|Application date=2010-02-10\|Standardized application number=2010WO-US23740\|Event publication date=2010-08-19\|Event code=WO/A2\|Event group=Examination events\|International application published with declaration under Article 17 (2) (a)\|Publication country=WO\|Publication number=WO2010093684\|Publication stage code=A2\|Publication date=2010-08-19\|Standardized publication number=WO201093684\|Event publication date=2010-11-18\|Event code=WO/A3\|Event indicator=Pos\|Event group=Examination events\|Later publication of ISR with revised front page\|Publication country=WO\|Publication number=WO2010093684\|Publication stage code=A3\|Publication date=2010-11-18\|Standardized publication number=WO201093684\|Event publication date=2012-08-12\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AP2011005878\|Actual or expected expiration date=2016-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=AP Corresponding appl: AP2011005878\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2011AP-0005878\|Corresponding cc:\|Designated or member state=AP Corresponding pat: AP2011005878\|Publication stage code in the designated or member state=A0\|Publication date in the 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state=2010-02-10\|Application number in the designated or member state=2010CA-2752524\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA2752524\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2010-08-19\|Publication number in the designated or member state=CA2752524\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CA\|Event publication date=2016-03-23\|Event code=CA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR CL\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=CL Corresponding appl: CL2011001962\|Event publication date=2011-08-11\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CL\|MEMBER STATE LEGAL DETAILS FOR CN102395657\|Actual or expected expiration date=2015-01-14\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN201080016478\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2010CN-80016478\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN102395657\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-03-28\|Publication number in the designated or member state=CN102395657\|Event publication date=2010-02-10\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CN\|Event publication date=2015-01-14\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2011-08-12\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2011-08-12\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR DZ\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=DZ Corresponding appl: DZDZP2011000597\|Event publication date=2011-09-08\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=DZ\|MEMBER STATE LEGAL DETAILS FOR EA201171023\|Actual or expected expiration date=2017-03-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EA Corresponding appl: EA201171023\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2011EA-0071023\|Corresponding cc:\|Designated or member state=EA Corresponding pat: EA201171023\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2012-03-30\|Publication number in the designated or member state=EA201171023\|Event publication date=2011-09-08\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EA\|Event publication date=2012-03-30\|Event code=EA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EA\|MEMBER STATE LEGAL DETAILS FOR EG26451\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=EG Corresponding appl: EG2011081359\|Application date in the designated or member state=2011-08-11\|Application number in the designated or member state=2011EG-0081359\|Corresponding cc:\|Designated or member state=EG Corresponding pat: EG26451\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2013-11-12\|Publication number in the designated or member state=EG--26451\|Event publication date=2013-11-12\|Event code=EG/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EG\|MEMBER STATE LEGAL DETAILS FOR EP2406353\|Actual or expected expiration date=2015-03-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP10741655\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2010EP-0741655\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2406353\|Publication stage code in the designated or member state=A2\|Publication date in the designated or member state=2012-01-18\|Publication number in the designated or member state=EP2406353\|Event publication date=2010-10-06\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2011-09-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2015-10-21\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR GE\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=GE Corresponding appl: GE12380\|Event publication date=2011-09-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=GE\|MEMBER STATE LEGAL DETAILS FOR IL214555\|Actual or expected expiration date=2016-09-27\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IL Corresponding appl: IL214555\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2010IL-0214555\|Corresponding cc:\|Designated or member state=IL Corresponding pat: IL214555\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-09-27\|Publication number in the designated or member state=IL-214555\|Event publication date=2011-08-09\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IL\|Event publication date=2011-09-27\|Event code=IL/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IL\|MEMBER STATE LEGAL DETAILS FOR IN1897/MUMNP/2011\|Actual or expected expiration date=2022-02-03\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN1897/MUMNP/2011\|Application date in the designated or member state=2011-09-10\|Application number in the designated or member state=2011IN-MN01897\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN1897/MUMNP/2011\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-02-03\|Publication number in the designated or member state=IN2011MN01897\|Event publication date=2011-09-10\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|Event publication date=2012-02-03\|Event code=IN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IN\|MEMBER STATE LEGAL DETAILS FOR MA33117\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=MA Corresponding appl: MA34162\|Application date in the designated or member state=2011-09-09\|Application number in the designated or member state=2011MA-0034162\|Corresponding cc:\|Designated or member state=MA Corresponding pat: MA33117\|Publication stage code in the designated or member state=B1\|Publication date in the designated or member state=2012-03-01\|Publication number in the designated or member state=MA--33117\|Event publication date=2012-03-01\|Event code=MA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=MA\|MEMBER STATE LEGAL DETAILS FOR MX2011008525\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=MX Corresponding appl: MX2011008525\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2011MX-0008525\|Corresponding cc:\|Designated or member state=MX Corresponding pat: MX2011008525\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-12-16\|Publication number in the designated or member state=MX2011008525\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=MX\|Event publication date=2014-04-24\|Event code=MX/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=MX\|MEMBER STATE LEGAL DETAILS FOR PE\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=PE Corresponding appl: PE001483-2011\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=PE\|MEMBER STATE LEGAL DETAILS FOR TN2011000396\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=TN Corresponding appl: TN2011000396\|Application date in the designated or member state=2011-08-09\|Application number in the designated or member state=2011TN-0000396\|Corresponding cc:\|Designated or member state=TN Corresponding pat: TN2011000396\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2013-03-27\|Publication number in the designated or member state=TN2011000396\|MEMBER STATE LEGAL DETAILS FOR UA104616\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=UA Corresponding appl: UAA201110768\|Application date in the designated or member state=2010-02-10\|Application number in the designated or member state=2011UA-0010768\|Corresponding cc:\|Designated or member state=UA Corresponding pat: UA104616\|Publication stage code in the designated or member state=C2\|Publication date in the designated or member state=2014-02-25\|Publication number in the designated or member state=UA-104616\|Event publication date=2014-02-25\|Event code=UA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=UA\|MEMBER STATE LEGAL DETAILS FOR ZA201106558\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=ZA Corresponding appl: ZA201106558\|Application date in the designated or member state=2011-09-07\|Application number in the designated or member state=2011ZA-0006558\|Corresponding cc:\|Designated or member state=ZA Corresponding pat: ZA201106558\|Publication stage code in the designated or member state=B\|Publication date in the designated or member state=2013-02-27\|Publication number in the designated or member state=ZA201106558\|Event publication date=2013-02-27\|Event code=ZA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=ZA\|(CN102395657)\|LEGAL DETAILS FOR CN102395657\|Actual or expected expiration date=2015-01-14\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201080016478\|Application date=2010-02-10\|Standardized application number=2010CN-80016478\|Event publication date=2012-03-28\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN102395657\|Publication stage code=A\|Publication date=2012-03-28\|Standardized publication number=CN102395657\|Event publication date=2012-03-28\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2012-05-09\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2015-01-14\|Event code=CN/WD01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent application deemed withdrawn after publication\|(GEP20146167)\|LEGAL DETAILS FOR GEP20146167\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-10\|Event code=GE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=GE GEAP2010012380\|Application date=2010-02-10\|Standardized application number=2010GE-0012380\|Event publication date=2014-09-25\|Event code=GE/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent for invention ( 2nd pub.)\|Publication country=GE\|Publication number=GEP20146167\|Publication stage code=B\|Publication date=2014-09-25\|Standardized publication number=GE201406167\|(MY152266)\|LEGAL DETAILS FOR MY152266\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-10\|Event code=MY/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MY MYPI2011003742\|Application date=2010-02-10\|Standardized application number=2011MY-0003742\|Event publication date=2014-09-15\|Event code=MY/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent / Utility Model\|Publication country=MY\|Publication number=MY152266\|Publication stage code=A\|Publication date=2014-09-15\|Standardized publication number=MY-152266\|(MX319678)\|LEGAL DETAILS FOR MX319678\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-10\|Event code=MX/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MX MX2011008525\|Application date=2010-02-10\|Standardized application number=2011MX-0008525\|Event publication date=2011-12-16\|Event code=MX/A\|Event group=Examination events\|Patent application\|Publication country=MX\|Publication number=MX2011008525\|Publication stage code=A\|Publication date=2011-12-16\|Standardized publication number=MX2011008525\|Event publication date=2014-04-24\|Event code=MX/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent/ granted utility model\|Publication country=MX\|Publication number=MX319678\|Publication stage code=B\|Publication date=2014-04-24\|Standardized publication number=MX-319678\|Event publication date=2014-04-24\|Event code=MX/FG\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant or registration\|Concesion\|(UA104616)\|LEGAL DETAILS FOR UA104616\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-10\|Event code=UA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=UA UAA201110768\|Application date=2010-02-10\|Standardized application number=2011UA-0010768\|Event publication date=2014-02-25\|Event code=UA/C2\|Event indicator=Pos\|Event group=Event indicating In Force\|Pat. grant. upon the USSR appl.,for which no pos. dec. made;grant. upon basis of national application\|Publication country=UA\|Publication number=UA104616\|Publication stage code=C2\|Publication date=2014-02-25\|Standardized publication number=UA-104616\|(EG26451)\|LEGAL DETAILS FOR EG26451\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-08-11\|Event code=EG/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EG EG2011081359\|Application date=2011-08-11\|Standardized application number=2011EG-0081359\|Event publication date=2013-11-12\|Event code=EG/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent for invention / Patent of addition\|Publication country=EG\|Publication number=EG26451\|Publication stage code=A\|Publication date=2013-11-12\|Standardized publication number=EG--26451\|(AU2010213862)\|LEGAL DETAILS FOR AU2010213862\|Actual or expected expiration date=2015-09-03\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=2010-02-10\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2010213862\|Application date=2010-02-10\|Standardized application number=2010AU-0213862\|Event publication date=2011-09-22\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2010213862\|Publication stage code=A1\|Publication date=2011-09-22\|Standardized publication number=AU2010213862\|Event publication date=2013-05-02\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent proceeded by OPI\|Publication country=AU\|Publication number=AU2010213862\|Publication stage code=B2\|Publication date=2013-05-02\|Standardized publication number=AU2010213862\|Event publication date=2013-08-29\|Event code=AU/FGA\|Event indicator=Pos\|Event group=Event indicating In Force\|Letters patent sealed or granted (standard patent)\|Event publication date=2015-09-03\|Event code=AU/MK14\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent ceased section 143(a) (annual fees not paid) or expired\|(ZA201106558)\|LEGAL DETAILS FOR ZA201106558\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-09-07\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA201106558\|Application date=2011-09-07\|Standardized application number=2011ZA-0006558\|Event publication date=2013-02-27\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA201106558\|Publication stage code=B\|Publication date=2013-02-27\|Standardized publication number=ZA201106558\|(MA33117)\|LEGAL DETAILS FOR MA33117\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-09-09\|Event code=MA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MA MA34162\|Application date=2011-09-09\|Standardized application number=2011MA-0034162\|Event publication date=2012-03-01\|Event code=MA/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=MA\|Publication number=MA33117\|Publication stage code=B1\|Publication date=2012-03-01\|Standardized publication number=MA--33117\|(BRPI1008447)\|LEGAL DETAILS FOR BRPI1008447\|Actual or expected expiration date=2019-10-01\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=BR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=BR BRPI1008447\|Application date=2010-02-10\|Standardized application number=2010BR-0008447\|Event publication date=2019-09-24\|Event code=BR/A2\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention / pipeline patent published without search report\|Publication country=BR\|Publication number=BRPI1008447\|Publication stage code=A2\|Publication date=2019-09-24\|Standardized publication number=BR201008447\|Event publication date=2019-10-01\|Event code=BR/B08F\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application fees: dismissal - article 86 of industrial property law\|Anuidade do pedido: arquivamento . Art. 86 da lpi [codigo 8.6 rpi]\|Event publication date=2020-01-21\|Event code=BR/B08K\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Lapse as no evidence of payment of the annual fee has been furnished to inpi (acc. art. 87)\|Manutencao do arquivamento [codigo 8.11 rpi]\|EM VIRTUDE DO ARQUIVAMENTO PUBLICADO NA RPI 2543 DE 01-10-2019 E CONSIDERANDO AUSENCIA DE MANIFESTACAO DENTRO DOS PRAZOS LEGAIS, INFORMO QUE CABE SER MANTIDO O ARQUIVAMENTO DO PEDIDO DE PATENTE, CONFORME O DISPOSTO NO ARTIGO 12, DA RESOLUCAO 113/2013.\|(TN2011000396)\|LEGAL DETAILS FOR TN2011000396\|Actual or expected expiration date=2030-02-10\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2011-08-09\|Event code=TN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=TN TN2011000396\|Application date=2011-08-09\|Standardized application number=2011TN-0000396\|Event publication date=2013-03-27\|Event code=TN/A1\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention\|Publication country=TN\|Publication number=TN2011000396\|Publication stage code=A1\|Publication date=2013-03-27\|Standardized publication number=TN2011000396\|(VE2010000234)\|LEGAL DETAILS FOR VE2010000234\|Actual or expected expiration date=2017-07-26\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-12\|Event code=VE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=VE VE2010-000234\|Application date=2010-02-12\|Standardized application number=2010VE-0000234\|Event publication date=2012-07-26\|Event code=VE/A\|Event indicator=Pos\|Event group=Examination events\|Patent Application or Foreign Patent Application\|Publication country=VE\|Publication number=VE2010000234\|Publication stage code=A\|Publication date=2012-07-26\|Standardized publication number=VE2010000234\|Event publication date=2017-07-26\|Event code=VE/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(PE20120704)\|LEGAL DETAILS FOR PE20120704\|Actual or expected expiration date=2016-05-30\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2010-02-10\|Event code=PE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=PE PE2011001483\|Application date=2010-02-10\|Standardized application number=2011PE-0001483\|Event publication date=2012-06-27\|Event code=PE/A1\|Event group=Examination events\|Patent application\|Publication country=PE\|Publication number=PE20120704\|Publication stage code=A1\|Publication date=2012-06-27\|Standardized publication number=PE201200704\|Event publication date=2016-05-30\|Event code=PE/FC\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Refusal\|Rechazada o denegada\|(EA201171023)\|LEGAL DETAILS FOR EA201171023\|Actual or expected expiration date=2017-03-30\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=EA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EA EA201171023\|Application date=2010-02-10\|Standardized application number=2011EA-0071023\|Event publication date=2012-03-30\|Event code=EA/A1\|Event group=Examination events\|Public. of applic. with search report\|Publication country=EA\|Publication number=EA201171023\|Publication stage code=A1\|Publication date=2012-03-30\|Standardized publication number=EA201171023\|Event publication date=2017-03-30\|Event code=EA/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IN1897/MUMNP/2011)\|LEGAL DETAILS FOR IN1897/MUMNP/2011\|Actual or expected expiration date=2022-02-03\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-09-10\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN1897/MUMNP/2011\|Application date=2011-09-10\|Standardized application number=2011IN-MN01897\|Event publication date=2012-02-03\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN1897/MUMNP/2011\|Publication stage code=A\|Publication date=2012-02-03\|Standardized publication number=IN2011MN01897\|Event publication date=2022-02-03\|Event code=IN/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(AP2011005878)\|LEGAL DETAILS FOR AP2011005878\|Actual or expected expiration date=2016-10-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=AP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AP AP2011005878\|Application date=2010-02-10\|Standardized application number=2011AP-0005878\|Event publication date=2011-10-31\|Event code=AP/A0\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=AP\|Publication number=AP2011005878\|Publication stage code=A0\|Publication date=2011-10-31\|Standardized publication number=AP2011005878\|Event publication date=2016-10-31\|Event code=AP/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IL214555)\|LEGAL DETAILS FOR IL214555\|Actual or expected expiration date=2016-09-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=IL/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IL IL214555\|Application date=2010-02-10\|Standardized application number=2010IL-0214555\|Event publication date=2011-09-27\|Event code=IL/A\|Event group=Examination events\|Application of patent for invention\|Publication country=IL\|Publication number=IL214555\|Publication stage code=A\|Publication date=2011-09-27\|Standardized publication number=IL-214555\|Event publication date=2016-09-27\|Event code=IL/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(CA2752524)\|LEGAL DETAILS FOR CA2752524\|Actual or expected expiration date=2016-02-10\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2752524\|Application date=2010-02-10\|Standardized application number=2010CA-2752524\|Event publication date=2010-08-19\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2752524\|Publication stage code=A1\|Publication date=2010-08-19\|Standardized publication number=CA2752524\|Event publication date=2016-03-23\|Event code=CA/FZDE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Dead\|Effective date of the event=2016-02-10	(EP2406353)\|Contracting States: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2010/093684)\|ARIPO: GH, GM, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2010/093684)\|EAPO: RU, TJ, BY, MD, AZ, TM, AM, KG, KZ\|(WO2010/093684)\|EPO: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2010/093684)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2010/093684)\|National States: PT, HN, HR, HU, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KM, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PE, PG, PH, PL	(WO2010/093684)\|CL; DZ; EG; GE; MA; MX; PE; TN; UA; ZA\|(GEP20146167)\|GE\|(MY152266)\|MY\|(MX319678)\|MX\|(UA104616)\|UA\|(EG26451)\|EG\|(ZA201106558)\|ZA\|(MA33117)\|MA\|(TN2011000396)\|TN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=jP3Nqvhw8TidMHrg3/9433mXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US8323481&ekey=935&xpn=EP2406353&kind=A4	https://register.epo.org/application?number=EP10741655	https://permalink.orbit.com/RenderStaticFirstPage?XPN=xq6OlXDbYJOeccOAsqvWAnfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2010/093684)\|US\|(US8323481)\|US	(WO2010/093684)\|NAME=RED LEAF RESOURCES, INC. 200 W. Civic Center Drive, Suite 190, Sandy, UT 84070 , COUNTRY=US\|(US8323481)\|NAME=Red Leaf Resources, Inc. , CITY=Sandy , STATE=UT , COUNTRY=US , ATYP=US Company	(EP2406353)\|DE\|(EP2406353)\|DE\|\|(US20100200465)\|US\|(WO2010/093684)\|US\|\|\|\|(AU2010213862)\|AU\|(AU2010213862)\|AU\|\|(CA2752524)\|CA	(EP2406353)\|NAME=Walker, Ross Thomson;Forresters Skygarden Erika-Mann-Strasse 11 , CITY=80636 München , COUNTRY=DE , REG=101298687\|(EP2406353)\|NAME=Walker, Ross Thomson;Forrester & Boehmert Pettenkoferstrasse 20-22 , CITY=80336 München , COUNTRY=DE , REG=100045009\|(US8323481)\|NAME=Thorpe North & Western LLP\|(US20100200465)\|NAME=THORPE NORTH & WESTERN, LLP. P.O. Box 1219 , CITY=SANDY , STATE=UT , POSTCODE=84091-1219 , COUNTRY=US\|(WO2010/093684)\|NAME=ERICKSEN, Erik S. et al. THORPE NORTH & WESTERN, LLP, P.O. Box 1219, Sandy, UT 84091-1219 , COUNTRY=US\|(CN102395657)\|NAME=ZHAO RONGMIN;JEEKAI & PARTNERS , REG=11245\|(MX319678)\|NAME=MARIA ANGELICA PARDAVELL JUAREZ\|(MX2011008525)\|NAME=MARIA ANGELICA PARDAVELL JUAREZ\|(AU2010213862)\|NAME=FB Rice Level 23 44 Market Street , CITY=SYDNEY , STATE=NSW , POSTCODE=2000 , COUNTRY=AU\|(AU2010213862)\|NAME=FB Rice Level 23 44 Market Street , CITY=Sydney , STATE=NSW , POSTCODE=2000 , COUNTRY=AU\|(VE2010000234)\|NAME=LINARES ALLOCA MARLIN ENEIDA\|(CA2752524)\|NAME=BERESKIN & PARR LLP/S.E.N.C.R.L.,S.R.L. , COUNTRY=CA	(EP2406353)\|US; US\|(EP2406353)\|US; US\|(US8323481)\|US; US\|(US20100200465)\|US; US\|\|(WO2010/093684)\|US; US\|\|\|\|(MX319678)\|US; US\|\|\|\|\|\|\|\|\|\|\|\|(IN1897/MUMNP/2011)\|US; US\|\|(CA2752524)\|US; US	(EP2406353)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, CITY=Park CityUT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., CITY=SandyUT 84092, COUNTRY=US\|(EP2406353)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, CITY=Park CityUT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., CITY=SandyUT 84092, COUNTRY=US\|(US8323481)\|NAME=Dana Todd, CITY=Park City, STATE=UT , COUNTRY=US \|NAME=Patten James W., CITY=Sandy, STATE=UT , COUNTRY=US\|(US20100200465)\|NAME=Dana Todd, CITY=Park City, STATE=UT , COUNTRY=US \|NAME=Patten James W., CITY=Sandy, STATE=UT , COUNTRY=US\|(WO2010/093684)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(WO2010/093684)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, Park City, UT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., Sandy, UT 84092, COUNTRY=US\|(CN102395657)\|NAME=DANA TODD\|NAME=PATTEN JAMES W.\|(GEP20146167)\|NAME=DANA, Todd\|NAME=PATTEN, James, W.\|(MY152266)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES W.\|(MX319678)\|NAME=TODD DANA, COUNTRY=US \|NAME=JAMES W PATTEN, COUNTRY=US\|(MX2011008525)\|NAME=TODD DANA\|NAME=JAMES W PATTEN\|(UA104616)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(EG26451)\|NAME=DANA TODD 3473 W. Daybreaker Drive Park City, UT 84098 (US)\|NAME=PATTEN JAMES W 4216 E. Wildcreek Rd. Sandy, UT 84092 (US)\|(AU2010213862)\|NAME=Dana, Todd\|NAME=Patten, James W.\|(AU2010213862)\|NAME=Dana, Todd\|NAME=Patten, James W.\|(ZA201106558)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(MA33117)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(BRPI1008447)\|NAME=James W. Patten\|NAME=Todd Dana\|(TN2011000396)\|NAME=PATTEN JAMES W.\|NAME=DANA TODD\|(VE2010000234)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(PE20120704)\|NAME=PATTEN, JAMES W.\|NAME=DANA, TODD\|(IN1897/MUMNP/2011)\|NAME=TODD DANA, COUNTRY=US \|NAME=PATTEN JAMES W, COUNTRY=US\|(AP2011005878)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(CA2752524)\|NAME=DANA, TODD, COUNTRY=US \|NAME=PATTEN, JAMES W., COUNTRY=US	(IN1897/MUMNP/2011)\|5\|(AU2010213862)\|5\|(CN102395657)\|5\|(CA2752524)\|5\|(US8323481)\|5	3	21		CARDINAL ENERGY HOLDINGS; FROM 2009-07-02; TO 2010-05-07	(EP2406353)\|WO2010/093684\|(CN102395657)\|WO2010/093684\|(MX319678)\|WO2010/093684\|(UA104616)\|WO2010/093684\|(EG26451)\|WO2010/093684\|(AU2010213862)\|WO2010/093684\|(ZA201106558)\|WO2010/093684\|(MA33117)\|WO2010/093684\|(BRPI1008447)\|WO2010/093684\|(TN2011000396)\|WO2010/093684\|(EA201171023)\|WO2010/093684\|(IN1897/MUMNP/2011)\|WO2010/093684\|(AP2011005878)\|WO2010/093684\|(IL214555)\|WO2010/093684\|(CA2752524)\|WO2010/093684		Primary examiner: Pardo Torre, J\|\|Primary examiner: Pardo Torre, J\|\|(US8323481)\|Number of Claims: NCL=12\|Number of Drawings: NDR=5\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=169\|Primary examiner: McCaig Brian\|Art Unit.: ART =1774\|\|(US20100200465)\|Number of Claims: NCL=26\|Number of Drawings: NDR=5\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1,14\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: McCaig Brian\|Art Unit.: ART =1774\|\|(WO2010/093684)\|Number of Claims: NCL=26\|Extended kind: EXTK=z\|\|(CN102395657)\|Number of Claims: NCL=26\|Gazette date: GAZDATE=2012-03-28\|Gazette number: GAZNUM=28-13\|Substantial examination effective date: 20120509\|Number of Pages: NPAGES=26\|\|(MX2011008525)\|Number of Claims: NCL=26\|Number of Pages: NPAGES=92\|\|(AU2010213862)\|Number of Claims: NCL=24\|\|(AU2010213862)\|Number of Claims: NCL=26\|\|(IN1897/MUMNP/2011)\|Number of Claims: NCL=26\|\|(AP2011005878)\|Gazette date: GAZDATE=2011-10-31\|\|(CA2752524)\|Number of Claims: NCL=26\|Number of Pages: NPAGES=46\|	(US8323481)\|Provisional Appl: US61/152,220 FDD=2009-02-12 [2009US-61152220]\|Previous publication: US20100200465 A1 2010-08-12 [US20100200465]	(EP2406353)\|ENGLISH (ENG)	(BR201008447)\|Patent\|(GE201406167)\|Patent\|(EP2406353)\|Patent\|(MY-152266)\|Patent\|(MX-319678)\|Patent\|(UA-104616)\|Patent\|(EG--26451)\|Patent\|(AU2010213862)\|Patent\|(TN2011000396)\|Patent\|(ZA201106558)\|Patent\|(US8323481)\|Patent\|(VE2010000234)\|Patent\|(PE201200704)\|Patent\|(EA201171023)\|Patent\|(CN102395657)\|Patent\|(MA--33117)\|Patent\|(IN2011MN01897)\|Patent\|(EP2406353)\|Patent\|(MX2011008525)\|Patent\|(AP2011005878)\|Patent\|(IL-214555)\|Patent\|(AU2010213862)\|Patent\|(WO201093684)\|Patent\|(CA2752524)\|Patent\|(WO201093684)\|Patent\|(US20100200465)\|Patent	Titre: (EP2406353)\|Carbon management and sequestration from encapsulated control infrastructures Résumé: (EP2406353)\|A method of sequestering carbon dioxide emissions during recovery of hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure (100). This constructed infrastructure (100) defines a substantially encapsulated volume. A comminuted hydrocarbonaceous material can be introduced into the control infrastructure (100) to form a permeable body (120) of hydrocarbonaceous material. The permeable body (120) can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure (100) is a fixed structure. Additionally, during heating, any carbon dioxide that is produced can be sequestered. Removed hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.	31	Abstract	gpt-4o-mini	no	The article focuses on carbon sequestration during hydrocarbon recovery, which does not involve accelerated weathering of minerals or the specific processes related to CO₂ capture through mineral alteration.
29	US63/469,108P\|US18/814,312\|US18/909,669\|WOUS2024/013913	US18/909,669\|WOUS2024/013913	US20250250199\|WO2024/248905	112475776	US20250250199 A1 2025-08-07 [US20250250199]\|WO2024/248905 A1 2024-12-05 [WO2024248905]	2023-05-26\|2024-02-01\|2024-08-23\|2024-10-08	2024-10-08\|2024-02-01	2025-08-07\|2024-12-05		(US20250250199)\|2044-02-01\|(WO2024/248905)\|2026-11-26	(US20250250199)\|Carbon-Sequestering Concrete Composition with Enhanced CO2 Absorbtion and Method of Manufacturing Thereof	(US20250250199)\|A carbon-sequestering concrete composition and method of production are disclosed. The composition comprises geopolymer binder components, aggregates, and alginate beads formed from brown algae powder through ionic gelation. The alginate beads significantly increase CO2 absorption surface area compared to algae powder, creating a matrix across the concrete surface that enhances long-term sequestration and improves durability. The beads interact synergistically with other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag, to enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The alginate beads also facilitate the dissolution of minerals like olivine, further enhancing carbon capture. The composition demonstrates superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. The method includes forming alginate beads, incorporating them into the concrete mixture, and allowing for initial hardening and drying processes that promote carbon dioxide absorption directly from the air.	LAFAVE MICHAEL ([US])\|LAFAVE MICHAEL ([US])	(US20250250199)\|Lafave Michael ([US])\|(WO2024/248905)\|LAFAVE, Michael ([US])	LAFAVE MICHAEL	(US20250250199)\|Lafave Michael	(WO2024/248905)\|SCHELL, Jeffrey ([US])	(US20250250199)\|The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture.\|This makes them significantly more effective for CO2 absorption compared to red and green algae species. The use of brown algae provides a more efficient and targeted approach to carbon sequestration in concrete, leveraging their natural adaptations to marine environments.\|By addressing the limitations of previous approaches, this invention represents a significant advancement in sustainable construction materials, offering superior carbon sequestration capabilities, enhanced durability, and improved overall performance.The preferred embodiment of the present invention addresses the limitations of previous approaches by utilizing brown algae species, particularly “Macrocystis pyrifera”, which have evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions.\|By incorporating these innovative features, the preferred embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|The preferred embodiment comprises a carbon-sequestering concrete and the associated methods of manufacture, addressing the limitations of previous methods and significantly enhancing CO2 absorption capabilities.\|	(US20250250199)\|1. A method of producing a carbon-sequestering concrete comprising: mixing sand and gravel aggregates while dry; adding and dry blending geopolymer binder components comprising at least one of slag, fly ash class C, fly ash class F, metakaolin, or silica fume; forming alginate beads by ionic gelation of brown algae powder; adding the alginate beads to the dry mixture of aggregates and geopolymer binder components; slowly incorporating water while mixing to achieve a workable concrete consistency; and pouring the concrete mixture into molds or forms for casting.\|6. A carbon-sequestering concrete composition comprising: 35-50% geopolymers comprising at least one of ground granulated blast furnace slag, class C fly ash, class F fly ash, metakaolin, or silica fume; 30-45% sand; 15-25% coarse aggregates comprising gravel or crushed stone; 5-10% water; and 1-5% alginate beads formed from brown algae powder.\|11. A carbon-sequestering concrete composition comprising: a geopolymer binder; aggregates; alginate beads formed from brown algae powder through ionic gelation; and at least one carbon dioxide sequestration enhancer selected from the group consisting of biochar, calcium carbonate, magnesium carbonate, magnesium silicate, olivine, and basalt rock dust.\|15. A carbon-sequestering concrete composition comprising: 30-60% aluminosilicate materials selected from the group consisting of: fly ash, ground granulated blast furnace slag, metakaolin, and silica fume; 30-50% CO2-absorbing materials selected from the group consisting of: magnesium silicate, olivine, biochar, calcium carbonate, and magnesium carbonate; 10-20% aggregates selected from the group consisting of: natural and recycled aggregates; 5-10% alkaline activators selected from the group consisting of: sodium hydroxide and sodium silicate; 5-15% algae-derived components selected from the group consisting of: silica from algae, algae biomass, and alginate beads; 1-5% carbonation accelerators; and 4-6% water; wherein the composition is capable of sequestering at least 400 kg of CO2 per 1,000 kg of concrete produced.\|	(US20250250199)\|The present invention relates to the field of sustainable construction materials, specifically to carbon-sequestering concrete compositions and methods for their production.\|The present invention seeks to overcome these limitations by providing a novel carbon-absorbing concrete composition and method of production that offers superior CO2 sequestration capabilities, enhanced durability, and improved overall performance compared to existing technologies.The present invention relates to a carbon-sequestering concrete composition and method of production that addresses the limitations of previous approaches to reducing the carbon footprint of concrete.\|	(US20250250199)\|ALGINATE BEAD(100,111)\|CARBON SEQUESTERING(100,25)\|CARBON SEQUESTERING CONCRETE(100,2)\|ENHANCED CO2 ABSORPTION(100,1)\|WORKABLE CONCRETE CONSISTENCY(72,1)\|SEQUESTRATION ENHANCER(60,1)\|SILICA FUME(57,9)\|IONIC GELATION(53,16)\|BLENDING GEOPOLYMER BINDER COMPONENT(49,1)\|CARBONATION ACCELERATOR(48,7)\|SUSTAINED CO2 ABSORPTION(47,3)\|GEOPOLYMER BINDER(46,4)\|GEOPOLYMER BINDER COMPONENT(46,2)\|CARBON DIOXIDE SEQUESTRATION ENHANCER(45,1)\|AGGREGATE(44,6)\|ALGAE BIOMASS(39,9)\|BROWN ALGAE POWDER(38,13)\|METAKAOLIN(37,11)\|BROWN ALGAE(35,28)\|ENHANCING DURABILITY(34,3)\|CO2 ABSORPTION(33,28)\|MACROCYSTIS PYRIFERA(31,11)\|NATURAL ADAPTATION(31,1)\|ALKALINE ACTIVATOR(30,3)\|RECYCLED AGGREGATE(29,6)\|SAND MIX(29,1)\|FLY ASH(28,21)\|BROWN ALGAE SPECIES(28,5)\|CO2 ABSORPTION CAPABILITY(27,2)\|LEVER AGING(27,1)\|CONCRETE(26,58)\|OLIVINE(25,23)\|SLAG(24,1)\|HARDENING(23,2)\|GEOPOLYMER COMPOUND(23,1)\|CO2 SEQUESTRATION CAPABILITY(22,11)\|CARBON SEQUESTRATION CAPABILITY(22,10)\|GREEN ALGAE SPECIES(22,2)\|BASALT(22,1)\|BIOCHAR(22,1)\|COARSE AGGREGATE(22,1)\|CRUSHED STONE(22,1)\|GEOPOLYMER(21,7)\|ALGINATE SOLUTION(20,10)\|SERVICE LIFE(20,10)\|MAGNESIUM SILICATE(20,9)\|ALGAE DERIVED COMPONENT(20,2)\|CONCRETE CARBON FOOTPRINT(20,2)\|GRAVEL(20,1)\|CARBON SEQUESTRATION(19,51)\|ACTIVATED BIOCHAR(19,2)\|SALT CONCENTRATION(19,2)\|MAGNESIUM CARBONATE(18,20)\|CASTING(18,1)\|BEAD(17,29)\|GROUND GRANULATED BLAST FURNACE SLAG(17,20)\|CALCIUM SILICATE HYDRATE(17,5)\|SEA CONDITION(17,2)\|ENHANCING CARBON CAPTURE(17,1)\|CALCIUM CARBONATE(16,22)\|CONCRETE TON(16,11)\|SYNERGISTIC INTERACTION(16,11)\|CROSSLINKING ION(16,4)\|GROUND OLIVINE(16,2)\|FLY ASH CLASS F(16,1)\|SAND(16,1)\|CONCRETE MATRIX(15,14)\|CRUCIAL ROLE(15,13)\|ALUMINOSILICATE MATERIAL(15,4)\|DUST(15,1)\|ALGAE(14,11)\|CONCRETE COMPONENT(14,9)\|SUPERPLASTICIZER(14,2)\|MARINE ENVIRONMENT(14,1)\|POROUS STRUCTURE(13,5)\|NEGATIVE NET CARBON FOOTPRINT(13,4)\|GEOPOLYMER BINDER FOUNDATION(13,2)\|CO2(12,28)\|CARBON DIOXIDE(12,24)\|CARBON DIOXIDE CAPTURE(12,10)\|NET NEGATIVE(12,4)\|POZZOLANIC REACTION ENHANCEMENT(12,4)\|CARBON FOOTPRINT(11,11)\|BASALT ROCK DUST(11,3)\|CARBON DIOXIDE ABSORPTION(11,2)\|GREEN ALGAE(11,2)\|CONCRETE SERVICE LIFE(10,6)\|MG2SIO(10,6)\|SODIUM SILICATE(10,6)\|CO2 ABSORBING MATERIAL(10,4)\|ECONOMIC VIABILITY(10,4)\|DRYING(10,2)\|MINERAL GRADUAL DISSOLUTION(10,2)\|ROBUST CELL WALL(10,2)\|SEED(10,1)\|CONCRETE MIXTURE(9,9)\|SODIUM HYDROXIDE(9,4)\|CLASS C FLY ASH(9,1)\|FLY ASH CLASS C(9,1)\|FORMED ALGINATE BEAD(9,1)\|OLIVINE GRADUAL DISSOLUTION(9,1)\|MOISTURE RETENTION(8,23)\|SELF HEALING(8,15)\|NATURAL AGGREGATE(8,6)\|ALGINATE POLYMER(8,4)\|BICARBONATE HCO3 ION(8,4)\|ADDITIVE CO2 SEQUESTRATION CAPABILITY(8,2)\|ALGINATE DROPLET(8,2)\|BEAD OPTIMIZATION(8,2)\|SPHERICAL ALGINATE BEAD FORMATION(8,2)\|ALGAE BIOMASS UPTAKE(8,1)\|CHEMICAL REACTION NATURE(8,1)\|CONCRETE PRODUCER FINANCIAL SITUATION(8,1)\|INNOVATIVE CONCRETE PRICE(8,1)\|LONG TERM SEQUESTRATION(7,8)\|SUSTAINABLE CONSTRUCTION MATERIAL(7,6)\|CONCRETE ABILITY(7,5)\|STABLE CARBONATE COMPOUND(7,5)\|CO2 DISSOLUTION(7,4)\|DROPLET SIZE(7,4)\|CONCRETE CARBON SEQUESTRATION CAPABILITY(7,3)\|AIR ENTRAIN(7,2)\|CONCRETE CURE(7,2)\|DISSOLVED CO2 INTERACTION(7,2)\|ENHANCING CO2 SEQUESTRATION(7,2)\|ADDITIVE GRADUAL DISSOLUTION(7,1)\|CLASS F FLY ASH(7,1)\|IMMENSE ENVIRONMENTAL BURDEN(7,1)\|CLASS F(6,6)\|CONCRETE FORMULATION(6,2)\|TAX BENEFIT(6,2)\|ACTIVATOR CAREFUL BALANCE(6,1)\|FINANCIAL INCENTIVE(6,1)\|TAX CREDIT ECONOMIC BENEFIT(6,1)\|CARBONIC ACID(5,9)\|CONCRETE STRUCTURE INTEGRITY(5,5)\|CARBON SEQUESTRATION POTENTIAL(5,4)\|WORKABILITY(5,4)\|ABSORB CO2(5,3)\|CO2 ABSORPTION PERIOD(5,3)\|CONCRETE CARBON CAPTURE CAPABILITY(5,3)\|CONCRETE PRODUCTION ENVIRONMENTAL IMPACT(5,3)\|CONCRETE STRENGTH(5,3)\|CLASS C(5,2)\|CONCRETE AGE(5,2)\|CONCRETE CAPABILITY(5,2)\|CONCRETE INTERNAL CURING(5,2)\|CREATING ALGINATE(5,2)\|CRITICAL INNOVATION(5,2)\|STABLE CARBONATE MINERAL(5,2)\|ALGAE CONCRETE TECHNOLOGY LIMITATION(5,1)\|ALGINATE BEAD ABILITY(5,1)\|ALGINATE BEAD UNIFORM DISTRIBUTION(5,1)\|BASALT DISSOLUTION(5,1)\|CARBON SEQUESTERING COMPETITIVENESS(5,1)\|CAREFUL DOCUMENTATION(5,1)\|CO2 CAPTURE(5,1)\|COMPOUND SEQUESTRATION(5,1)\|CONCRETE INTEGRITY(5,1)\|CONCRETE LIFESPAN(5,1)\|CONCRETE MIXER INVESTMENT(5,1)\|CONCRETE OPTION(5,1)\|CONCRETE OVERALL SEQUESTRATION CAPACITY(5,1)\|CONCRETE SUSCEPTIBILITY(5,1)\|DERIVED ALGINATE BEAD(5,1)\|ENHANCE CO2 UPTAKE(5,1)\|ENHANCE CONCRETE CO2 SEQUESTRATION CAPABILITY(5,1)\|ENHANCING CO2 ABSORPTION(5,1)\|GEOPOLYMER PRECURSOR(5,1)\|MAXIMIZE CO2 SEQUESTRATION CAPABILITY(5,1)\|MAXIMIZE ELIGIBILITY(5,1)\|METAKAOLIN INCLUSION(5,1)\|NET EARNINGS SEQUESTRATION(5,1)\|PROLONGED SEQUESTRATION(5,1)\|RELEVANT REGULATORY REQUIREMENT(5,1)\|SCIENTIFIC APPARATUS RESERVOIR(5,1)\|SEAWATER INCORPORATION(5,1)\|STABLE CALCIUM CARBONATE FORMATION(4,7)\|CONCRETE DURABILITY(4,6)\|PERIOD EXTENSION(4,6)\|ACCOUNTING(4,3)\|CURING PERIOD(4,3)\|INVESTMENT TAX CREDIT(4,3)\|IONIC GELATION(4,3)\|TONNE(4,3)\|BICARBONATE ION(4,2)\|NET CARBON SEQUESTRATION(4,2)\|STRUCTURAL REQUIREMENT(4,2)\|SUSTAINABLE CONSTRUCTION PRACTICE(4,2)\|ABSORBED CO2(4,1)\|ACCELERATION STRENGTH GAIN(4,1)\|APPLICABLE INCENTIVE(4,1)\|APPLICABLE TAX CREDIT(4,1)\|CAPTURED CO2 REMAINS(4,1)\|CARBON SEQUESTERING ADOPTION(4,1)\|CO2 ABSORPTION SITE(4,1)\|CO2 EMISSION(4,1)\|CONCRETE MIXTURE SUSTAINABILITY(4,1)\|CRACK REPAIR(4,1)\|DRIED ALGAE POWDER(4,1)\|ENHANCED ALGINATE BEAD FORMATION(4,1)\|ENHANCED CO2 SEQUESTRATION CAPABILITY(4,1)\|ENHANCING REACTIVITY(4,1)\|FUCUS SPECIES(4,1)\|INVENTOR OBSERVATION(4,1)\|MAGNESIUM ION RELEASE(4,1)\|MOIST ENVIRONMENT(4,1)\|MOISTURE ABSORPTION(4,1)\|PORE INTERCONNECTION(4,1)\|PROJECT REQUIREMENT(4,1)\|RAPID CARBONATION REACTION(4,1)\|SEQUESTERING CARBON(4,1)\|SILICA DISSOLUTION(4,1)\|SILICA FUME FINE PARTICLE(4,1)\|TON BATCH(4,1)\|TRACE MINERAL(4,1)\|LOCALIZED HIGH HUMIDITY ENVIRONMENT(3,17)\|CALCIUM HYDROXIDE(3,4)\|DROPWISE(3,4)\|NAOH(3,4)\|CALCIUM ALUMINATE HYDRATE(3,2)\|CAPTURING CARBON DIOXIDE(3,2)\|CEMENT HYDRATION(3,2)\|CONCRETE MIXTURE REQUIREMENT(3,2)\|DIVALENT CATION(3,2)\|EARLY STRENGTH(3,2)\|EXCESS ION(3,2)\|MAGNESIUM CARBONATE FORMATION(3,2)\|STATE TAX INCENTIVE(3,2)\|ACTIVE CO2 ABSORPTION(3,1)\|ADDRESS ENVIRONMENTAL CONCERN(3,1)\|ADJUSTED PARAMETER(3,1)\|ALGINATE CONTENT(3,1)\|APPLICABLE REGULATION(3,1)\|CALCIUM CARBONATE PRECIPITATE(3,1)\|CARBON CAPTURE OPPORTUNITY(3,1)\|CARBON CAPTURING CONCRETE(3,1)\|CARBON DIOXIDE GIGATON(3,1)\|CO2 ABSORPTION INCONSISTENT LEVEL(3,1)\|CO2 SEQUESTRATION POTENTIAL(3,1)\|CO2 UPTAKE RATE(3,1)\|COMBINED TAX CREDIT(3,1)\|CONCRETE CARBON CAPTURE CAPACITY(3,1)\|CONCRETE CO2 ABSORPTION CAPACITY(3,1)\|CONTRIBUTOR(3,1)\|DEPICTION(3,1)\|DISCRETE PARTICLE(3,1)\|EMISSION SCALE(3,1)\|EXPERIMENTATION(3,1)\|EXTENDED ABSORPTION WINDOW(3,1)\|FEAT(3,1)\|INCREASED MINERAL CARBONATION POTENTIAL(3,1)\|INNOVATIVE ALGAE DERIVED COMPONENT(3,1)\|MAXIMIZE CO2 ABSORPTION CAPACITY(3,1)\|MICROCRACK(3,1)\|MIXED ALGAE(3,1)\|MIXING ALGAE(3,1)\|MOISTURE RETENTION ENHANCEMENT(3,1)\|RELEASED MAGNESIUM ION(3,1)\|SOLID ALGAE POWDER PARTICLE(3,1)\|STABLE MINERAL(3,1)\|STARK CONTRAST(3,1)\|SUSTAINABLE SILICA SOURCE(3,1)\|CONSTRUCTION MATERIAL(2,7)\|GEOPOLYMERIZATION(2,3)\|INCREASED MOISTURE CONTENT(2,3)\|KEY COMPONENT(2,2)\|\|(WO2024/248905)\|CARBON DIOXIDE(100,42)\|GEOPOLYMER CONCRETE(100,21)\|CARBON SEQUESTERING(100,10)\|SIDEWALK(100,10)\|ATMOSPHERIC CARBON DIOXIDE(100,8)\|BINDER(100,8)\|DRIED MARINE ALGA POWDER(100,7)\|CARBON SEQUESTERING GEOPOLYMER CONCRETE(100,4)\|CARBON SEQUESTERING CONCRETE(100,2)\|SIDEWALK CARBON SEQUESTERING(100,1)\|DRIED MARINE ALGA(94,9)\|GEOPOLYMERIC BINDER PRECURSOR(83,1)\|ALKALINE ACTIVATOR(70,4)\|FINISHED PEDESTRIAN INFRASTRUCTURE(69,1)\|SILICA FUME(67,10)\|WORKABLE CONCRETE CONSISTENCY(64,2)\|INNATE CO2 AFFINITY(61,1)\|FREEZE THAW RESILIENCE(60,4)\|GEOPOLYMER ALGAE CONCRETE SLAB(59,1)\|SERVICE LIFETIME(58,4)\|INTERGROUND LIMESTONE INCORPORATION(57,1)\|COARSE AGGREGATE(56,14)\|BLENDING GEOPOLYMER BINDER COMPONENT(56,1)\|METAKAOLIN(51,6)\|GEOPOLYMER ALGAE CONCRETE MIXTURE(51,2)\|SIDEWALK SEGMENT(51,1)\|ENHANCED FREEZE THAW RESILIENCE(49,1)\|FINE AGGREGATE(48,6)\|GEOPOLYMER BINDER(46,7)\|MARINE MACROALGAE(46,3)\|FRESHWATER SPECIES(44,1)\|CARBON MINERALIZATION REACTION(42,1)\|ENHANCED CARBON MINERALIZATION(41,4)\|CONCRETE SLAB MATRIX(41,1)\|CRITICAL URBAN GROWTH(41,1)\|RENEWAL EFFORT(41,1)\|SIDEWALK ADOPTION(41,1)\|RE USE(40,1)\|SIDEWALK SEGMENT SHAPE(39,1)\|SAND MIX(37,2)\|GEOPOLYMER(36,24)\|GEOPOLYMER PRECURSOR(36,7)\|LOGISTICAL BARRIER(36,2)\|FUCUS SPECIES(35,3)\|ALGAE ADDITIVE(35,2)\|LIMESTONE POWDER(35,2)\|PERIODIC WETTING(35,2)\|GEOPOLYMERIC BINDER PHASE(34,2)\|ALKALI ACTIVATOR(33,3)\|ALGAE POWDER(32,17)\|FLY ASH(31,17)\|ANGULAR CRUSHED PARTICLE(31,1)\|INTEGRATED ALGAE POWDER(31,1)\|CONCRETE(30,46)\|GEOPOLYMER BINDER COMPONENT(30,4)\|ATMOSPHERIC CARBON DIOXIDE MINERALIZATION(30,1)\|ALGINATE POLYMER(29,4)\|THICKNESS CONCRETE SLAB(29,1)\|AGGREGATE(28,10)\|GROUND GRANULATED BLAST FURNACE SLAG(27,10)\|ALKALI ACTIVATOR SOLUTION(27,4)\|DRIED ALGAE(27,3)\|DRIED SALT(27,1)\|LB CARBON DIOXIDE(27,1)\|CONCRETE MIXTURE(26,9)\|CEMENTITIOUS MATERIAL(26,8)\|ECO FRIENDLY CONSTRUCTION(26,1)\|EXTENDED DURABILITY(26,1)\|STABLE CALCIUM CARBONATE(26,1)\|CARBON DIOXIDE EMISSION(25,4)\|DOLOMITIC SAND(25,3)\|INTEGRATED DRIED MARINE ALGA(25,1)\|GEOPOLYMER MATRIX(24,5)\|MARINE ALGA(24,5)\|LAMINARIA(24,3)\|DURATION EXTENSION(24,2)\|ALGAE DERIVED CALCIUM ION(24,1)\|CONCRETE SLAB(24,1)\|SEA SALT(23,16)\|CO2 ABSORPTION(23,13)\|CO2 ABSORBING CONCRETE(23,3)\|MAGNESIUM ION(22,6)\|CALCIUM OXIDE POWDER(22,3)\|DRYING CYCLE(22,2)\|GEOPOLYMER COMPOUND(22,2)\|ASCOPHYLLUM(21,3)\|TRANSPORTATION COST(21,3)\|COARSE AGGREGATE INTRODUCTION(21,2)\|GREENHOUSE EMISSION(21,1)\|REACTIVE AGGREGATE MATERIAL(21,1)\|CUBIC YARD(20,4)\|DRY MIXER BLEND(20,4)\|MAGNESIUM OXIDE POWDER(20,4)\|SARGASSUM(20,3)\|SLAB(20,2)\|COMPOSITION CURE(20,1)\|CUMULATIVE REMOVAL(20,1)\|BINDER MATRIX(18,9)\|ENHANCING DURABILITY(18,2)\|WORKABILITY TARGETED LEVEL(18,2)\|FLY ASH CLASS F(18,1)\|MEASURED INCREMENT(18,1)\|CRUSHED STONE(17,4)\|ADOPTION(17,2)\|FINISHING EQUIPMENT(17,2)\|INLAND CONSTRUCTION SITE(17,2)\|PACKING DENSITY CONSOLIDATION(17,2)\|CARBON DIOXIDE TON(17,1)\|CARBON NEGATIVE PERFORMANCE CREDENTIALS(17,1)\|WINTER CONDITION(17,1)\|SEAWATER(16,17)\|SODIUM SILICATE(16,4)\|LIFETIME(16,3)\|CARBON DIOXIDE LB(16,1)\|LARGE CONSUMER(16,1)\|STANDARD CONCRETE MIX(16,1)\|SLAG(15,8)\|SODIUM HYDROXIDE(15,4)\|CASTING(15,3)\|FINAL CONCRETE(15,3)\|SEAWATER LARGE VOLUME(15,1)\|URBAN PEDESTRIAN INFRASTRUCTURE RENEWAL(15,1)\|SAND(14,12)\|CALCIUM OXIDE REACTIVITY(14,2)\|SEMIANGULAR SHAPE(14,2)\|REACTIVE MAGNESIUM OXIDE(14,1)\|CO2(13,32)\|GRAVEL(13,6)\|ALUMINOSILICATE SOURCE MATERIAL(13,2)\|PREVENT LOCALIZED SETTING(13,1)\|CALCIUM OXIDE(12,13)\|MAGNESIUM OXIDE(12,11)\|MAGNESIUM CARBONATE(12,4)\|INTERRUPTION(12,3)\|BROWN ALGAE GROUP(12,2)\|CALCIUM ION(12,2)\|CALCIUM CARBONATE(11,6)\|DRIED MARINE SALT(11,6)\|CONCRETE MIXER(11,2)\|TARGET LEVEL(11,2)\|BURNING ANTHRACITE BYPRODUCT(11,1)\|BYPRODUCT GEOPOLYMER INCORPORATION(11,1)\|EQUIPMENT LIFETIME(11,1)\|GEOPOLYMERIC ALUMINOSILICATE PRECURSOR(11,1)\|INTRINSIC MINERAL CARBONATION REACTIVITY(11,1)\|METAKAOLIN GEOPOLYMER BINDER(11,1)\|MITIGATE SUSTAINABILITY ISSUE(11,1)\|OCEAN ECOSYSTEM DEPLETION(11,1)\|CONCRETE MATRIX(10,5)\|GEOPOLYMERIZATION REACTION(10,5)\|MGO AVAILABILITY(10,3)\|ALUMINOSILICATE MATERIAL(10,2)\|SIDEWALK SLAB(10,2)\|METAKAOLIN GEOPOLYMERIC BINDER(10,1)\|CLASS C FLY ASH(9,7)\|DURABLE INFRASTRUCTURE(9,2)\|GEOPOLYMERIC PRECURSOR(9,2)\|LOGISTICAL CHALLENGE(9,2)\|PRODUCTIVE REUSE(9,2)\|AGGREGATE SUITABLENESS EVALUATION(9,1)\|ALGAL BIOMASS ASH(9,1)\|ALGAL COMPOUND BIORECEPTIVITY(9,1)\|CARBON DIOXIDE ABSORPTION CAPACITY(9,1)\|CONCRETE OVER CUBIC YARD(9,1)\|GLOBAL EMISSION INFRASTRUCTURE SHARE(9,1)\|HYBRID GEOPOLYMER ALGAE CONCRETE(9,1)\|MARINE SEAWATER ALGAE(9,1)\|PEDESTRIAN INFRASTRUCTURE PROJECT(9,1)\|REPURPOSING INDUSTRIAL BYPRODUCT(9,1)\|URBAN ROAD INFRASTRUCTURE(9,1)\|CARBON ABSORBING GEOPOLYMER CONCRETE(8,5)\|DRIED ALGAE POWDER(8,3)\|MINERAL REACTION(8,3)\|PARTICLE SIZE(8,3)\|CEMENT COMPONENT(8,2)\|CHEMICAL REACTION NATURE(8,2)\|CONCRETE WORKABILITY(8,2)\|EMISSION POUND(8,2)\|FLY ASH CLASS C(8,2)\|MAJOR COMPATIBILITY ISSUE(8,2)\|BYPRODUCT TON(8,1)\|GEOPOLYMER ALGAE CONCRETE CURE(8,1)\|GEOPOLYMER ALGAE CONCRETE FORMULATION(8,1)\|GEOPOLYMER CONSTITUENT CARBONATE(8,1)\|GEOPOLYMERIZATION POLYMER CROSSLINKING(8,1)\|IMMENSE ENVIRONMENTAL BURDEN(8,1)\|OPTIMIZED GEOPOLYMER ALGAE CONCRETE(8,1)\|ROAD CO2 FOOTPRINT(8,1)\|SLOW SEAWATER DIFFUSION KINETICS(8,1)\|SUSTAINABLE AQUACULTURE(8,1)\|VISUAL MICROSTRUCTURAL VERIFICATION(8,1)\|CLASS F FLY ASH(7,5)\|ALGAL COMPONENT(7,4)\|CARBONATION POTENTIAL(7,2)\|CONCRETE USAGE(7,2)\|FAST GROWING(7,2)\|AGGREGATE HOMOGENEOUS DISPERSION(7,1)\|ALGAE CO2 ABSORPTION(7,1)\|ALGAL BIOMASS MINERAL COMPOSITE(7,1)\|BYPRODUCT SLAG(7,1)\|CARBON MINERALIZE ALGAL BIOMASS(7,1)\|CARBONATION KINETICS(7,1)\|DRIED ALGAE REHYDRATE(7,1)\|INVENTOR ALGAE ADDITIVE(7,1)\|LIFECYCLE THREAT(7,1)\|MEETING STRINGENT PURITY(7,1)\|MILE INLAND(7,1)\|MINERAL CARBONATION SITE(7,1)\|PERSISTENT CARBON MINERALIZATION(7,1)\|SEAWATER HUNDRED ENORMOUS VOLUME(7,1)\|SELECTIVE PRESSURE(7,1)\|SLAG BALANCED BLEND(7,1)\|TRANSPORTABLE MARINE SALT(7,1)\|UNIFORMLY GRADED AGGREGATE(7,1)\|WIDESCALE ADOPTION(7,1)\|WIDESPREAD COMMERCIAL ADOPTION(7,1)\|CURING(6,4)\|EARLY STRENGTH(6,3)\|LARGE VOLUME(6,3)\|ALGAE BEARING GEOPOLYMER CONCRETE(6,2)\|CARBONATE PRECIPITATION(6,2)\|CARBONATION REACTION(6,2)\|CELL WALL(6,2)\|CLASS F(6,2)\|CO2 UPTAKE CAPACITY(6,2)\|CURING CONCRETE(6,2)\|DRYING(6,2)\|MECHANICAL STRENGTH(6,2)\|MINERAL CARBONATE FORMATION(6,2)\|WATER BINDER RATIO(6,2)\|ACTIVELY ABSORB AMBIENT CO2(6,1)\|ACTIVELY ABSORBING CO2(6,1)\|ALGAE BIOMASS ASH(6,1)\|ALGAL ASH(6,1)\|ALGAL BIOMASS CONTENT(6,1)\|CANDIDATE SAND TESTING(6,1)\|CARBON DIOXIDE OVER(6,1)\|CARBON MINERALIZATION FUNCTIONALITY(6,1)\|CARBONATE DIFFRACTION PEAK INTENSITY(6,1)\|CARBONATION CURING(6,1)\|CO2 EMISSION TON(6,1)\|CO2 EMISSION YEAR(6,1)\|CO2 ENHANCING DIFFUSION(6,1)\|CONTINUAL CULTIVATION(6,1)\|CRUSHED SAND PARTICLE(6,1)\|DOLOMITIC AGGREGATE(6,1)\|DYNAMICS COMPETITION(6,1)\|ECONOMIC BINDER OPTION(6,1)\|ENHANCED CO2 MINERALIZATION CAPACITY(6,1)\|ENHANCING MATRIX COHESION(6,1)\|ERECTED ONSITE(6,1)\|FELDSPATHIC SAND(6,1)\|FRESHWATER ALGA SPECIES(6,1)\|GEOPOLYMER CONCRETE LEVERAGE(6,1)\|HARDENED GEOPOLYMER CONCRETE(6,1)\|INNATE REACTIVITY(6,1)\|INTEGRATING SEAWATER(6,1)\|LIMESTONE DERIVED CAO(6,1)\|LOGISTICS BARRIER(6,1)\|LOGISTICS CONSTRAINT(6,1)\|MASSIVE SCALABILITY(6,1)\|MAXIMIZED CARBON MINERALIZATION(6,1)\|MEANINGFUL CO2 SEQUESTRATION(6,1)\|MGO PRECURSOR SITE(6,1)\|MINERAL CARBONATION CAPACITY(6,1)\|MULTIYARD BUCKET(6,1)\|PETROGRAPHIC EXAMINATION(6,1)\|PLENTIFUL CAO(6,1)\|REALISTIC VARIABILITY(6,1)\|RECYCLING PATHWAY(6,1)\|ROBUST CROSSLINKED MATRIX(6,1)\|SALINITY OCEAN ENVIRONMENT(6,1)\|SAND MINERALOGY(6,1)\|SIDEWALK LIFETIME(6,1)\|SIDEWALK SQUARE FOOT(6,1)\|SUBBITUMINOUS COAL BURNING(6,1)\|TRANSPORTATION IMPEDIMENT(6,1)\|WIDESPREAD ADOPTION(6,1)\|BINDER PHASE(5,3)\|CARBON DIOXIDE UPTAKE(5,3)\|PRIMARY BINDER(5,3)\|UNIFORM DISTRIBUTION(5,3)\|ALGAE CONTENT(5,2)\|CA DISSOLUTION(5,2)\|CO2 CAPTURE(5,2)\|CONCRETE CARBON FOOTPRINT(5,2)\|CONCRETE MANUFACTURER(5,2)\|CONCRETE PERFORMANCE(5,2)\|CONSTRUCTION SCHEDULE(5,2)\|EMISSION SCALE(5,2)\|FINAL DRY INGREDIENT(5,2)\|SUSTAINABLE INFRASTRUCTURE(5,2)\|ABUNDANT CAO(5,1)\|AGGREGATE PROPORTION(5,1)\|ALGAE BLEND(5,1)\|ALGAE SPECIES(5,1)\|ALGAL ADDITIVE(5,1)\|BINDER CONSOLIDATION(5,1)\|BLENDED GEOPOLYMER BINDER COMPONENT(5,1)\|BUILDING CONCRETE REQUIREMENT(5,1)\|CARBONATE SAND(5,1)\|CIVIC CONSTRUCTION INITIATIVE(5,1)\|CO2 POUND(5,1)\|CO2 PRECIPITATION(5,1)\|COARSE AGGREGATE PURITY(5,1)\|COMPATIBILITY CHALLENGE(5,1)\|COMPOSITIONAL MODIFICATION(5,1)\|COMPREHENSIVE EVALUATION(5,1)\|CONCRETE COMPONENT(5,1)\|CONCRETE CONSISTENCY(5,1)\|CONCRETE DRY INGREDIENT(5,1)\|CONCRETE DURABILITY(5,1)\|CONCRETE POUND(5,1)\|DISSOLVED CALCIUM ABUNDANCE(5,1)\|DRY CONCRETE CONSTITUENT(5,1)\|DURABLE SANDSTONE(5,1)\|EMISSION MITIGATION(5,1)\|EMISSION QUARTER(5,1)\|ENORMOUS EMISSION(5,1)\|EXTERIOR HARDSCAPE(5,1)\|FERROSILICON ALLOY(5,1)\|FINE LIMESTONE POWDER(5,1)\|GEOPOLYMER ALGAE CONCRETE MIX(5,1)\|GEOPOLYMERIC GEL(5,1)\|GROWING MARINE ALGA(5,1)\|HEAVY AGGREGATE(5,1)\|HIGHWAY INTEGRITY(5,1)\|HIGHWAY PROFILE(5,1)\|HIGHWAY STRETCHING(5,1)\|HOMOGENIZE FULL COMPLEMENT(5,1)\|IMPACTFUL ROUTE(5,1)\|INCORPORATED ALGAL BIOMASS(5,1)\|INFRASTRUCTURE EXPANSION(5,1)\|LIBERATED CO2(5,1)\|MAJOR CONCRETE INGREDIENT(5,1)\|MAJOR UNRESOLVED BARRIER(5,1)\|MAXIMIZE CARBON MINERALIZATION POTENTIAL(5,1)\|MEASURABLE PROGRESS(5,1)\|MICROALGAL POWDER(5,1)\|MINERAL SUITABILITY(5,1)\|NATURAL POZZOLAN(5,1)\|NET CO2 EMISSION(5,1)\|NET CO2 IMPACT(5,1)\|OFFSET MINOR IMPURITY(5,1)\|OPTIMIZED AGGREGATE SELECTION(5,1)\|OPTIMIZED REACTIVITY(5,1)\|REACTIVE BINDER IDEAL(5,1)\|SCALABLE PATHWAY(5,1)\|SCARCE LANDFILL VOLUME(5,1)\|SEAWATER CARBON ABSORPTION(5,1)\|SLAG BINDER(5,1)\|SLAG PRECURSOR(5,1)\|STRUCTURAL INFRASTRUCTURE(5,1)\|SUN DRYING(5,1)\|THERMOGRAVIMETRIC ANALYSIS(5,1)\|VARIANCE LOCALIZATION(5,1)\|WASH GRADING(5,1)\|CLASS C(4,10)\|CACO3(4,5)\|CONCRETE STRENGTH(4,5)\|MGCO3(4,5)\|ALGINATE POLYMER CHAIN(4,2)\|ALKALI SOLUTION(4,2)\|CARBON ABSORBING CONCRETE(4,2)\|CARBON DIOXIDE POUND(4,2)\|COMPONENT REACTION(4,2)\|DEFICIT(4,2)\|DEMOLDING(4,2)\|ENOUGH CALCIUM(4,2)\|FINE POWDER(4,2)\|HEAT GENERATION(4,2)\|INCOMPATIBILITY(4,2)\|PORTLAND CEMENT(4,2)\|SEA CONDITION(4,2)\|STANDARD CONCRETE MANUFACTURE(4,2)\|TRANSPORTATION INFRASTRUCTURE(4,2)\|WALKWAY(4,2)\|ABSORBED CO2(4,1)\|ABSORPTION KINETICS(4,1)\|ABUNDANT CALCIUM(4,1)\|ABUNDANT CO2(4,1)\|ABUNDANT GLOBAL SUPPLY(4,1)\|ABUNDANT ION(4,1)\|ACTIVATOR PARAMETER(4,1)\|AGGREGATE PARTICLE(4,1)\|AIRBORNE CO2(4,1)\|ALGAE DISPERSION(4,1)\|ALGAE POWDER PRODUCTION(4,1)\|ALKALI ACTIVATED ALUMINOSILICATE CHEMISTRY(4,1)\|BINDER COMPONENT INITIATE DISSOLUTION(4,1)\|BINDER INGREDIENT(4,1)\|BINDER PASTE(4,1)\|BLEND BALANCE(4,1)\|BROAD ADOPTION(4,1)\|CARBON MINERALIZATION CAPACITY(4,1)\|CHUTE DISCHARGE(4,1)\|CO2 NATURAL DIFFUSION(4,1)\|CO2 TON(4,1)\|COAL COMBUSTION(4,1)\|CONCRETE CURING(4,1)\|CONCRETE POWDER SAMPLE(4,1)\|CONCRETE SERVICE LIFE(4,1)\|CUMULATIVE CO2 REMOVAL(4,1)\|DEVELOPING CARBONATE(4,1)\|DRY AGGREGATING MIXING(4,1)\|DRYING SHRINKAGE(4,1)\|ENHANCED DIFFUSION(4,1)\|ENHANCED LONGEVITY(4,1)\|EVENLY DISTRIBUTED CAO CONTENT(4,1)\|EXTENDED SERVICE LIFETIME(4,1)\|FAST KINETICS(4,1)\|FULL BINDER BLEND CONTEXT(4,1)\|FULL CO2 MINERALIZATION CAPACITY(4,1)\|GEOPOLYMER PERFORMANCE(4,1)\|GEOPOLYMER RATIO(4,1)\|GEOPOLYMERIC COMPONENT(4,1)\|GEOPOLYMERIC COMPOUND(4,1)\|GRADE COMPACTION(4,1)\|GRADING ZONE(4,1)\|GRAVEL PARTICLE(4,1)\|GRAVIMETRIC TESTING(4,1)\|GREENHOUSE GAS RERELEASE(4,1)\|HARDENING DURATION(4,1)\|INTEGRATED MARINE SALT(4,1)\|LANDFILL LOADING(4,1)\|LANDFILL WASTE VOLUME(4,1)\|LIFECYCLE PERFORMANCE(4,1)\|MAJOR CONTRIBUTOR(4,1)\|MAJOR ECONOMIC LIMITATION(4,1)\|MAKE GEOPOLYMER CONCRETE(4,1)\|MARINE ALGA INTEGRATION(4,1)\|MASSIVE CONCRETE VOLUME(4,1)\|MASSIVE DEMAND(4,1)\|MAXIMIZE SERVICE LIFE(4,1)\|MGO REACTION(4,1)\|MIXING AGGREGATE(4,1)\|NATURAL MINERALIZATION(4,1)\|NEGATION CAPABILITY(4,1)\|OPTIMUM CONSISTENCY(4,1)\|PARTICLE DURABILITY(4,1)\|PERSISTENT CARBON SEQUESTRATION(4,1)\|PLURAL INCLUSION(4,1)\|POLYCONDENSATION REACTION(4,1)\|PORTABLE MIXER(4,1)\|POZZOLANIC QUALITY(4,1)\|PRECIPITATED CARBONATE COMPOUND(4,1)\|PRECIPITATED CARBONATE FORMATION(4,1)\|PROCESSED MARINE SALT(4,1)\|REACTIVE CAO(4,1)\|REACTIVE MINERAL ION(4,1)\|REBAR SPACING(4,1)\|RELIABLE CO2 SEQUESTRATION(4,1)\|REQUIRING REINFORCEMENT(4,1)\|ROBUST CO2(4,1)\|ROUNDED GRAIN(4,1)\|ROUNDED PARTICLE(4,1)\|SAND PROPORTION(4,1)\|SEAWATER SALT(4,1)\|SPECIALIZED CONTAINER(4,1)\|STAGNANT MICROSCOPIC WATER(4,1)\|SUPPORTING SUSTAINABILITY(4,1)\|THROUGHOUT INTACT CONCRETE SAMPLE(4,1)\|TRANSPORTATION DEPARTMENT PROJECT(4,1)\|WORKABLE MATRIX FORMATION(4,1)\|ABLE INLAND DISTRIBUTION(3,1)\|ALGAE DERIVED CALCIUM(3,1)\|ALKALI ACTIVATED SLAG(3,1)\|ALKALI ACTIVATION REACTION(3,1)\|ALKALINE ACTIVATOR SOLUTION(3,1)\|ANGULAR PARTICLE(3,1)\|ASTM CL(3,1)\|BINDER ADJUSTMENT(3,1)\|BINDER ALONE ACCOUNT(3,1)\|BINDER MANUFACTURING(3,1)\|BINDER REACTION(3,1)\|BLENDING QUALITY(3,1)\|BONDING ENHANCEMENT(3,1)\|CA REACTION(3,1)\|CALCIUM CARBONATE STABILIZATION(3,1)\|CALCIUM ION ABUNDANCE(3,1)\|CAPTURING CARBON(3,1)\|CARBAMATE FORMATION(3,1)\|CARBON DIOXIDE GIGATON(3,1)\|CARBON ENHANCED CURING REGIME(3,1)\|CARBONATE LOCK(3,1)\|CO2 ABSORPTION INCONSISTENT LEVEL(3,1)\|CO2 ABSORPTION MEANINGFUL LEVEL(3,1)\|CO2 CURING(3,1)\|CO2 LB CONCRETE(3,1)\|CO2 UPTAKE RATE(3,1)\|COASTAL ACCESS(3,1)\|CONTINUING CARBON SEQUESTRATION(3,1)\|CONTROLLED ADDITION(3,1)\|DEPICTION(3,1)\|DIVALENT CALCIUM ION(3,1)\|DRY COMPONENT(3,1)\|DRY INCORPORATION(3,1)\|DURABLE MATRIX(3,1)\|ECO FRIENDLY PRODUCTION(3,1)\|EMBODIED CARBON ABSORPTION(3,1)\|FINITE NATURAL RESOURCE(3,1)\|FLATWORK(3,1)\|FRACTURE FACE(3,1)\|GEOPOLYMER PRODUCTION(3,1)\|GLOBAL EMISSIONS REDUCTION TARGET(3,1)\|HARDENED STRENGTH(3,1)\|HARDENING REACTION(3,1)\|HEAT BUILDUP(3,1)\|HOMOGENEOUS MIXING(3,1)\|HYDROXIDE ION(3,1)\|IMMENSE CARBON REDUCTION OPPORTUNITY(3,1)\|INCONSISTENT PERFORMANCE(3,1)\|INSTALLATION CARBON ABSORPTION(3,1)\|INTERDEPENDENT CHEMICAL INTERACTION(3,1)\|KEYING(3,1)\|LIMIT FEASIBILITY(3,1)\|MANUFACTURED SAND(3,1)\|MAP CARBONATE(3,1)\|MASS ALGAE(3,1)\|MINERAL DELIVERY(3,1)\|MIXER RUN(3,1)\|NATURAL SAND(3,1)\|NEUTRAL PH(3,1)\|OPERATIONAL LIMITATION(3,1)\|ORGANIC IMPURITY(3,1)\|ORGANIC MINIMIZATION(3,1)\|PERFORMING CURING(3,1)\|PORE NETWORK(3,1)\|PRIMARY CONCRETE(3,1)\|PRODUCTION POUND(3,1)\|QUALITY GRAVEL(3,1)\|RAPID ADOPTION(3,1)\|REACTION CAPABILITY(3,1)\|READY MIX CONCRETE PRODUCTION(3,1)\|RELEASING CALCIUM(3,1)\|RELIABLE CARBON ABSORPTION(3,1)\|RENEWABLE SUPPLY(3,1)\|SALT CONCENTRATION(3,1)\|SEAWATER SOLUTION(3,1)\|SIDEWALK CONSTRUCTION ENVIRONMENTAL IMPACT(3,1)\|SIEVING(3,1)\|SILICA SAND(3,1)\|STABLE CARBONATE COMPOUND(3,1)\|STRENGTH BUILDUP(3,1)\|SUSTAINABLE HARVEST(3,1)\|TOTAL BINDER BLEND(3,1)\|TRANSFORMATIVE(3,1)\|UNIFORM AGGREGATE DISTRIBUTION(3,1)\|UNIFORM BLEND(3,1)\|URBAN SCALE(3,1)\|	(US20250250199)\|I claim:\|1. A method of producing a carbon-sequestering concrete comprising:\| mixing sand and gravel aggregates while dry;\| adding and dry blending geopolymer binder components comprising at least one of slag, fly ash class C, fly ash class F, metakaolin, or silica fume;\| forming alginate beads by ionic gelation of brown algae powder;\| adding the alginate beads to the dry mixture of aggregates and geopolymer binder components;\| slowly incorporating water while mixing to achieve a workable concrete consistency; and\| pouring the concrete mixture into molds or forms for casting.\|2. The method of claim 1, wherein forming the alginate beads comprises:\| mixing brown algae powder with water to create an alginate solution;\| introducing the alginate solution dropwise into a bath containing calcium ions; and\| collecting the formed alginate beads.\|3. The method of claim 2, wherein the brown algae powder is derived from Macrocystis pyrifera. \|4. The method of claim 1, further comprising controlling the size and density of the alginate beads by adjusting at least one of: concentration of the alginate solution, type and concentration of crosslinking ions, and droplet size.\|5. The method of claim 1, further comprising allowing an initial hardening and drying process during which the alginate beads absorb carbon dioxide directly from the air through natural chemical reactions with the geopolymer compounds.\|6. A carbon-sequestering concrete composition comprising:\| 35-50% geopolymers comprising at least one of ground granulated blast furnace slag, class C fly ash, class F fly ash, metakaolin, or silica fume;\| 30-45% sand;\| 15-25% coarse aggregates comprising gravel or crushed stone;\| 5-10% water; and\| 1-5% alginate beads formed from brown algae powder.\|7. The composition of claim 6, wherein the alginate beads are formed through ionic gelation of brown algae powder derived from Macrocystis pyrifera. \|8. The composition of claim 6, further comprising at least one of magnesium carbonate and olivine (Mg2SiO4).\|9. The composition of claim 6, wherein the alginate beads create a matrix across the surface of the concrete, increasing carbon dioxide absorption surface area compared to algae powder.\|10. The composition of claim 6, wherein the alginate beads contribute to self-healing of micro-cracks in the concrete by facilitating ongoing formation of carbonate compounds.\|11. A carbon-sequestering concrete composition comprising:\| a geopolymer binder;\| aggregates;\| alginate beads formed from brown algae powder through ionic gelation; and\| at least one carbon dioxide sequestration enhancer selected from the group consisting of biochar, calcium carbonate, magnesium carbonate, magnesium silicate, olivine, and basalt rock dust.\|12. The carbon-sequestering concrete composition of claim 11, wherein the geopolymer binder comprises at least one of fly ash, ground granulated blast furnace slag, metakaolin, or silica fume.\|13. The carbon-sequestering concrete composition of claim 11, wherein the alginate beads are formed from brown algae species Macrocystis pyrifera. \|14. The carbon-sequestering concrete composition of claim 11, further comprising carbonation accelerators in the form of calcium silicate hydrate (C—S—H) seeds.\|15. A carbon-sequestering concrete composition comprising:\| 30-60% aluminosilicate materials selected from the group consisting of: fly ash, ground granulated blast furnace slag, metakaolin, and silica fume;\| 30-50% CO2-absorbing materials selected from the group consisting of: magnesium silicate, olivine, biochar, calcium carbonate, and magnesium carbonate;\| 10-20% aggregates selected from the group consisting of: natural and recycled aggregates;\| 5-10% alkaline activators selected from the group consisting of: sodium hydroxide and sodium silicate;\| 5-15% algae-derived components selected from the group consisting of: silica from algae, algae biomass, and alginate beads;\| 1-5% carbonation accelerators; and\| 4-6% water;\| wherein the composition is capable of sequestering at least 400 kg of CO2 per 1,000 kg of concrete produced.\|16. The carbon-sequestering concrete composition of claim 15, wherein the aluminosilicate materials comprise 30% fly ash (Class F), 20% ground granulated blast furnace slag, 5% metakaolin, and 3% silica fume.\|17. The carbon-sequestering concrete composition of claim 15, wherein the CO2-absorbing materials comprise 15% magnesium silicate, 15% finely ground olivine, 10% activated biochar, 3% calcium carbonate, and 2% magnesium carbonate.\|18. The carbon-sequestering concrete composition of claim 15, wherein the algae-derived components comprise 1% silica from algae, 3% algae biomass for bead formation, and 5% alginate beads.\|19. The carbon-sequestering concrete composition of claim 15, further comprising 0.5% superplasticizers and 0.1% air-entraining agents.\|20. The carbon-sequestering concrete composition of claim 15, wherein the composition has a net negative carbon footprint of at least 300 kg CO2 per 1,000 kg of concrete produced.	(US20250250199)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] This application claims the benefit of and incorporates by reference in its entirety U.S. Provisional Patent Application No. 63/469,108, filed May 26, 2023 which is incorporated herein by reference in its entirety. This application also claims the benefit of, is a continuation-in-part of, and incorporates by reference in its entirety U.S. patent application Ser. No. 18/722,678, filed on Jun. 21, 2024, and U.S. patent application Ser. No. 18/814,312 filed on Aug. 23, 2024. This application also claims the benefit of and incorporates by reference in its entirety International Patent Application No. PCT/US24/13913, filed Feb. 1, 2024.\|(US20250250199)\|FIELD OF THE INVENTION\|[0002] The present invention relates to the field of sustainable construction materials, specifically to carbon-sequestering concrete compositions and methods for their production.\|BACKGROUND OF THE INVENTION\|[0003] Concrete is one of the most widely used construction materials globally, with over 4 billion metric tons produced annually.\|[0004] However, conventional Portland cement concrete production is a significant contributor to global carbon dioxide emissions, accounting for 7-8% of all CO2 emissions worldwide. This represents an immense environmental burden, generating over 2 gigatons of carbon dioxide per year during cement production alone.\|[0005] Recent efforts to mitigate the carbon footprint of concrete have explored various approaches, including the incorporation of seawater and algae into concrete mixes to enable CO2 sequestration.\|[0006] However, these existing methods have achieved only modest and inconsistent levels of CO2 absorption that pale in comparison to the scale of emissions from concrete production.\|[0007] One such approach is described in Korean Patent No. 102079643 B1 to Lee et al. (“LEE”), which discloses a carbon dioxide-absorbing marine concrete composition made by mixing blast furnace slag, fly ash, metakaolin, sodium silicate, and dried algae powder. While this composition attempts to address the environmental impact of concrete production, it suffers from several significant limitations.\|[0008] The use of algae powder alone in the manner disclosed by LEE fails to fully leverage the carbon sequestration potential of marine algae, as it does not provide optimal surface area for CO2 absorption or create the necessary conditions for long-term carbon mineralization. Furthermore, simply mixing algae powder into concrete does not facilitate the formation of a matrix across the concrete surface that could enhance long-term sequestration and improve durability. There is a need for an innovative approach that can dramatically increase the CO2 absorption capacity of concrete, create synergistic interactions with other concrete components, and provide a mechanism for moisture retention to facilitate greater direct air capture of CO2. Such an approach would overcome the limitations of current algae-based concrete technologies and offer superior CO2 sequestration capabilities, enhanced durability, and improved overall performance.\|[0009] The need for carbon-capturing concrete has become increasingly urgent as the construction industry seeks to reduce its significant carbon footprint. To incentivize the adoption of such environmentally beneficial technologies, various tax credits and incentives have been established. Section 45Q of the Internal Revenue Code provides tax credits for carbon oxide sequestration, which can result in substantial savings for concrete producers utilizing this technology. Additionally, the Investment Tax Credit offers up to 30% credit on capital investments in carbon-capturing technologies. Other applicable incentives include R&D tax credits, Production Tax Credits, and various federal and state tax incentives designed to promote sustainable construction practices. These financial incentives not only make the adoption of carbon-sequestering concrete more economically viable but also align with broader policy goals of reducing greenhouse gas emissions and promoting sustainable development in the construction industry.\|[0010] These limitations result in a concrete composition that, while attempting to address environmental concerns, falls short of achieving significant and long-lasting carbon sequestration. The present invention seeks to overcome these limitations by providing a novel carbon-absorbing concrete composition and method of production that offers superior CO2 sequestration capabilities, enhanced durability, and improved overall performance compared to existing technologies.\|SUMMARY OF THE INVENTION\|[0011] The present invention relates to a carbon-sequestering concrete composition and method of production that addresses the limitations of previous approaches to reducing the carbon footprint of concrete.\|[0012] At the core of the preferred embodiment is the utilization of brown algae species, particularly “Macrocystis pyrifera”, which are transformed into alginate beads through a process called ionic gelation. These alginate beads dramatically increase the surface area available for CO2 absorption, forming a matrix across the concrete surface that enhances long-term sequestration and improves durability.\|[0013] The alginate beads are created through ionic gelation using brown algae powder. This process involves mixing the algae powder with water to create an alginate solution, which is then introduced dropwise into a bath containing calcium ions. As the droplets come into contact with the calcium ions, they undergo rapid gelation, forming stable, three-dimensional network structures with a high surface area, ideal for CO2 absorption and moisture retention in concrete.\|[0014] The preferred embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0015] The alginate beads play a crucial role in moisture retention in the context of the preferred embodiment, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0016] The preferred embodiment also addresses the formation of bicarbonate (HCO3-) ions in the presence of moisture from alginate beads, which is crucial for the carbon sequestration mechanism of the concrete. This process contributes to the concrete's ability to sequester CO2 not only during the initial curing phase but also throughout its service life.\|[0017] Furthermore, the alginate beads contribute to the self-healing of micro-cracks in the concrete, extending its lifespan and durability. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0018] In summary, the preferred embodiment provides a concrete composition with superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. It addresses the limitations of previous approaches and represents a significant advancement in sustainable construction materials.\|(US20250250199)\|BRIEF DESCRIPTION OF THE FIGURES\|[0019] FIG. 1 depicts the usage of an embodiment of the invention in association with a sidewalk.\|[0020] FIG. 2 depicts the usage of an embodiment of the invention in association with a pillar associated with a typical construction project.\|(US20250250199)\|DETAILED DESCRIPTION\|[0021] The preferred embodiment comprises a carbon-sequestering concrete and the associated methods of manufacture, addressing the limitations of previous methods and significantly enhancing CO2 absorption capabilities.\|[0022] At the core of this embodiment is the utilization of brown algae species, particularly “Macrocystis pyrifera”, which are transformed into alginate beads through a process called ionic gelation. These alginate beads dramatically increase the surface area available for CO2 absorption, forming a matrix across the concrete surface that enhances long-term sequestration and improves durability. The alginate beads in the preferred embodiment are created through a process called ionic gelation using brown algae powder, particularly from species “Macrocystis pyrifera”. This process is critical for enhancing CO2 absorption in the concrete mixture.\|[0023] The brown algae species “Macrocystis pyrifera” was chosen for creating alginate beads in the preferred embodiment due to its superior carbon sequestration capabilities. This species has evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions, making it significantly more effective for CO2 absorption compared to red and green algae species. The alginate extracted from Macrocystis pyrifera is particularly rich in carboxyl groups, which are crucial for the ionic gelation process used to form the beads. When mixed with water and introduced dropwise into a calcium ion bath, the alginate from Macrocystis pyrifera forms stable, three-dimensional network structures with a high surface area, ideal for CO2 absorption and moisture retention in concrete. In alternative embodiments, other brown algae species may serve as a substitute, including but not limited to Laminaria, Ascophyllum, Sargassum, and Fucus species. These alternative species also possess similar cell wall structures and carbon-binding capabilities, although Macrocystis pyrifera remains the preferred choice due to its particularly high alginate content and optimal gelation properties for concrete applications.\|[0024] To form the alginate beads, the brown algae powder is first mixed with water to create an alginate solution. This solution contains the alginate polymers naturally present in the cell walls of brown algae, which are rich in carboxyl groups.\|[0025] The alginate solution in an embodiment is then introduced dropwise into a bath containing divalent cations, typically calcium ions. As the alginate droplets come into contact with the calcium ions, they undergo a rapid gelation process. The calcium ions crosslink the alginate polymers, forming a stable, three-dimensional network structure. This ionic gelation process results in the formation of spherical alginate beads with a significantly increased surface area compared to the original algae powder. The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture. The ionic gelation process for forming alginate beads in an embodiment begins with mixing brown algae powder, particularly from species like “Macrocystis pyrifera”, with water to create an alginate solution. This solution contains the alginate polymers naturally present in the cell walls of brown algae, which are rich in carboxyl groups. The alginate solution is then introduced dropwise into a bath containing divalent cations, typically calcium ions. As the alginate droplets come into contact with the calcium ions, they undergo a rapid gelation process. The calcium ions crosslink the alginate polymers, forming a stable, three-dimensional network structure. This process results in the formation of spherical alginate beads with a significantly increased surface area compared to the original algae powder. The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture. The size and density of the alginate beads can be controlled by adjusting various parameters during the gelation process, such as the concentration of the alginate solution, the type and concentration of the crosslinking ions, and the droplet size. This allows for optimization of the beads' properties to suit the specific requirements of the concrete mixture. Once formed, the alginate beads are collected and may undergo further processing, such as washing to remove excess ions and drying to a desired moisture content. The resulting beads are then ready to be incorporated into the concrete mixture, where they will play a crucial role in enhancing CO2 sequestration and improving the overall performance of the concrete in accordance with an embodiment of the invention.\|[0026] The size and density of the alginate beads can be controlled by adjusting various parameters during the gelation process, such as the concentration of the alginate solution, the type and concentration of the crosslinking ions, and the droplet size. This allows for optimization of the beads' properties to suit the specific requirements of the concrete mixture.\|[0027] Once formed, the alginate beads are collected and may undergo further processing, such as washing to remove excess ions and drying to a desired moisture content. The resulting beads are then ready to be incorporated into the concrete mixture, where they will play a crucial role in enhancing CO2 sequestration and improving the overall performance of the concrete.\|[0028] The formation of these alginate beads through ionic gelation is a key innovation that sets the preferred embodiment of the invention apart from previous approaches that simply mixed algae powder into concrete. The beads provide a matrix across the surface of the concrete, dramatically enhancing long-term sequestration and improving the concrete's durability.\|[0029] The alginate beads formed from brown algae powder significantly increase the CO2 absorption surface area compared to simply using algae powder in concrete. This enhancement in surface area is achieved through the ionic gelation process, which creates a porous, three-dimensional structure within each bead.\|[0030] When algae powder is directly mixed into concrete in accordance with the preferred embodiment, it remains as discrete particles with limited surface area exposed for CO2 interaction. In contrast, the alginate beads form a matrix across the surface of the concrete, dramatically increasing the total surface area available for carbon dioxide absorption.\|[0031] The ionic gelation process creates a network of interconnected pores within each alginate bead. This porous structure allows CO2 molecules to penetrate deep into the bead, rather than just interacting with the outer surface. As a result, the effective surface area for CO2 absorption is multiplied many times over compared to solid algae powder particles in accordance with the preferred embodiment.\|[0032] Furthermore, the alginate beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. This moisture retention further enhances CO2 absorption, as the carbonation process reacts more readily in the presence of water. The combination of increased surface area and moisture retention allows for significantly more efficient CO2 capture and conversion to stable carbonate compounds.\|[0033] The size and density of the alginate beads can be controlled during the gelation process in accordance with various embodiments, allowing for optimization of the surface area to volume ratio. By adjusting parameters such as alginate concentration, crosslinking ion type and concentration, and droplet size, the beads can be tailored to maximize their CO2 absorption capacity.\|[0034] Additionally, the alginate beads create a more uniform distribution of CO2 absorption sites throughout the concrete matrix compared to algae powder. This even distribution ensures that the carbon sequestration potential is maximized across the entire concrete structure, rather than being limited to localized areas where algae powder particles might cluster.\|[0035] The cumulative effect of these factors in accordance with the preferred embodiment-increased surface area, porous structure, moisture retention, and uniform distribution-results in CO2 absorption capabilities that are orders of magnitude greater than what can be achieved with simple algae powder incorporation associated with other attempts. This dramatic enhancement in carbon sequestration efficiency is a critical innovation of the preferred embodiment of the invention, enabling concrete structures to serve as highly effective carbon sinks throughout their service life.\|[0036] The preferred embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS).\|[0037] These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption. The alginate beads also play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2.\|[0038] The preferred embodiment enhances pozzolanic reactions through the synergistic interaction between alginate beads and various components of the concrete mix, particularly fly ash and metakaolin.\|[0039] Pozzolanic reactions occur when siliceous or aluminosiliceous materials react with calcium hydroxide in the presence of water to form compounds with cementitious properties. In the context of this invention, the alginate beads create localized high-humidity environments within the concrete matrix, which facilitates these reactions. The increased moisture content provided by the beads promotes the dissolution of silica and alumina from the pozzolanic materials, allowing them to react more readily with calcium hydroxide produced during the hydration of cement or geopolymer precursors. This enhanced reactivity leads to the formation of additional calcium silicate hydrate (C—S—H) and calcium aluminate hydrate (C-A-H) gels, which contribute to the concrete's strength and durability. Furthermore, the pozzolanic reactions consume calcium hydroxide, reducing the concrete's susceptibility to chemical attacks and improving its long-term performance. The increased pozzolanic activity also creates more sites for carbon dioxide capture within the concrete composition, as the newly formed C—S—H and C-A-H gels provide additional surface area for CO2 absorption and carbonation.\|[0040] The preferred embodiment creates additional sites for carbon dioxide capture through several mechanisms. The alginate beads formed from brown algae powder increase the surface area available for CO2 absorption, creating a matrix across the concrete surface that enhances long-term sequestration. This matrix structure provides numerous additional sites for CO2 to interact with and be captured by the concrete. Furthermore, the synergistic interactions between the alginate beads and other concrete components, such as fly ash and ground granulated blast furnace slag (GGBFS), lead to enhanced pozzolanic reactions in association with the preferred embodiment.\|[0041] These reactions create more sites in the concrete composition specifically for capturing carbon dioxide. The increased pozzolanic activity results in the formation of additional calcium silicate hydrate (C—S—H) and calcium aluminate hydrate (C-A-H) gels, which provide extra surface area for CO2 absorption and carbonation. The alginate beads also interact positively with other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4).\|[0042] The alginate beads in the preferred embodiment interact synergistically with additives like magnesium carbonate and olivine (Mg2SiO4) to enhance the concrete's CO2 sequestration capabilities. The moisture retention properties of the alginate beads play a crucial role in facilitating these interactions.\|[0043] For magnesium carbonate, the localized high-humidity environments created by the alginate beads promote its gradual dissolution within the concrete matrix. This dissolution process releases magnesium ions, which can then react with dissolved CO2 to form stable magnesium carbonate compounds, effectively capturing and storing atmospheric carbon dioxide.\|[0044] In the case of olivine (Mg2SiO4), the humidity retained by the alginate beads creates conditions favorable for its dissolution in accordance with the preferred embodiment. As the olivine dissolves, it releases magnesium ions into the concrete matrix. These magnesium ions can then interact with the alginate structure, enhancing the formation of magnesium carbonates. This process not only contributes to additional CO2 sequestration but also improves the overall strength and durability of the concrete.\|[0045] The alginate beads create “localized high-humidity environments” within the concrete through their unique moisture absorption and retention properties. When incorporated into the concrete mixture, these beads absorb and hold water, acting as microscopic reservoirs distributed throughout the concrete matrix.\|[0046] In accordance with the preferred embodiment, as the concrete cures and ages, the alginate beads continue to retain this moisture, creating small pockets of high humidity surrounding each bead. These localized high-humidity environments are crucial for facilitating CO2 absorption, as the carbonation process reacts more readily in the presence of water. The retained moisture provides a medium for atmospheric CO2 to dissolve, forming carbonic acid which then interacts with calcium ions to produce stable calcium carbonate. This process of CO2 absorption and carbonate formation is significantly enhanced by the consistent availability of moisture provided by the alginate beads, allowing for continuous carbon sequestration throughout the concrete's service life. Furthermore, these high-humidity microenvironments promote the gradual dissolution of other additives like magnesium carbonate and olivine, further enhancing the concrete's overall CO2 absorption capacity.\|[0047] The continuous moisture provision by the alginate beads ensures that these reactions can occur over an extended period, prolonging the concrete's carbon capture capabilities. As atmospheric CO2 dissolves in the water retained by the beads, it forms carbonic acid, which then reacts with the magnesium ions released from both magnesium carbonate and olivine to produce stable carbonate compounds. These interactions between the alginate beads and additives like magnesium carbonate and olivine create a self-sustaining cycle of CO2 absorption and mineralization within the concrete. The process continues throughout the concrete's service life, significantly enhancing its long-term carbon sequestration potential compared to traditional concrete compositions.\|[0048] The preferred embodiment prolongs the period of CO2 absorption through several innovative mechanisms. The alginate beads formed from brown algae powder play a crucial role in extending the carbon sequestration capabilities of the concrete over time. These beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix that facilitate ongoing CO2 absorption.\|[0049] The synergistic interactions between the alginate beads and other concrete components, such as ground granulated blast furnace slag (GGBFS), increase both the hydration and carbonation processes. This effectively extends the duration during which the concrete can actively absorb carbon dioxide from the atmosphere.\|[0050] Furthermore, the alginate beads enhance the CO2 sequestration capabilities of other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4). The humidity retained by the beads creates conditions that promote the gradual dissolution of these minerals, leading to sustained carbon capture over an extended period. The continuous process of CO2 absorption is supported by the ongoing formation of carbonate compounds within the concrete matrix.\|[0051] The alginate beads facilitate the dissolution of minerals including olivine (Mg2SiO4) to enhance carbon capture through several mechanisms. The beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. This increased moisture content promotes the gradual dissolution of olivine, releasing magnesium ions into the surrounding concrete. The humidity in the alginate beads creates these localized high moisture environments, which are crucial for facilitating olivine dissolution. As the olivine dissolves, the released magnesium ions interact with the alginate structure, enhancing the formation of magnesium carbonates. This process not only contributes to additional CO2 sequestration but also improves the overall strength and durability of the concrete. The continuous moisture provision by the alginate beads ensures that these reactions can occur over an extended period, prolonging the concrete's carbon capture capabilities. Furthermore, the beads provide additional surface area for basalt dissolution, which leads to further carbon capture. This synergistic interaction between the alginate beads and olivine creates a self-sustaining cycle of CO2 absorption and mineralization within the concrete, significantly enhancing its long-term carbon sequestration potential compared to traditional concrete compositions.\|[0052] As atmospheric CO2 dissolves in the water retained by the alginate beads, it forms carbonic acid, which then reacts with calcium ions to produce stable calcium carbonate. This cycle of absorption and mineralization continues throughout the concrete's service life, significantly prolonging its CO2 sequestration capabilities.\|[0053] Additionally, the formation of stable calcium carbonate contributes to the self-healing of micro-cracks in the concrete. This self-healing property not only extends the overall lifespan of the concrete but also maintains its ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure. The alginate beads also contribute to the self-healing of micro-cracks in the concrete through several mechanisms. As the concrete cures and ages, the alginate beads continue to absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. When micro-cracks form, these moist environments facilitate the ongoing formation of carbonate compounds. As atmospheric CO2 dissolves in the water retained by the alginate beads, it forms carbonic acid, which then reacts with calcium ions to produce stable calcium carbonate. This calcium carbonate precipitates within the micro-cracks, gradually filling them and restoring the concrete's integrity. The continuous nature of this process, enabled by the moisture-retaining properties of the alginate beads, allows for ongoing self-healing throughout the concrete's service life. Additionally, the alginate beads' ability to enhance pozzolanic reactions and create additional sites for carbon dioxide capture contributes to the formation of supplementary binding materials that can further aid in crack repair. This self-healing property not only extends the overall lifespan of the concrete but also maintains its ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0054] By incorporating these innovative features, the preferred embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0055] The humidity retained by the alginate beads creates localized high moisture environments that facilitate the dissolution of these minerals, leading to further carbon capture opportunities. This process increases the overall number of sites available for CO2 sequestration within the concrete matrix. Lastly, the moisture retention properties of the alginate beads create conditions favorable for the ongoing formation of carbonate compounds throughout the concrete.\|[0056] As CO2 dissolves in the water absorbed by the beads, it forms carbonic acid, which then interacts with calcium ions to form stable calcium carbonate. This continuous process effectively creates new sites for carbon dioxide capture as the concrete ages, prolonging its CO2 sequestration capabilities over time.\|[0057] This innovative concrete composition not only reduces the carbon footprint associated with production but also actively removes CO2 from the atmosphere throughout its service life. The carbon capture process in the preferred embodiment occurs strongly over the initial approximately 60 days due to the rapid initial reactions between the alginate beads and atmospheric CO2, but continues on a smaller scale for many years thereafter.\|[0058] This prolonged sequestration is enabled by several key mechanisms:\|[0059] During the initial curing period, the alginate beads formed through ionic gelation provide a large surface area for CO2 absorption, allowing for rapid carbonation reactions. The beads absorb and retain moisture, creating localized high-humidity environments that facilitate the dissolution of CO2 and its reaction with calcium ions to form stable calcium carbonate.\|[0060] As the concrete continues to age, the synergistic interactions between the alginate beads and other components of the mix, such as ground granulated blast furnace slag (GGBFS) and fly ash, sustain the carbon capture process. These interactions lead to ongoing pozzolanic reactions and the creation of additional sites for CO2 absorption, albeit at a slower rate than during the initial curing period.\|[0061] The moisture retention properties of the alginate beads play a crucial role in maintaining conditions favorable for long-term CO2 sequestration. Even as the concrete ages, the beads continue to absorb and retain water from the environment, providing a medium for CO2 to dissolve and react with available calcium ions.\|[0062] Furthermore, the formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete. This self-healing process not only extends the lifespan of the concrete but also maintains pathways for continued CO2 absorption over many years.\|[0063] The gradual dissolution of minerals such as magnesium carbonate and olivine, facilitated by the moisture retained in the alginate beads, provides a slow but steady source of reactive components for ongoing CO2 sequestration. This process continues at a reduced rate long after the initial curing period, allowing the concrete to capture carbon dioxide from the atmosphere throughout its service life.\|[0064] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions in the alginate beads contributes to the self-healing of micro-cracks, further extending the concrete's lifespan and durability. By addressing the limitations of previous approaches, this invention represents a significant advancement in sustainable construction materials, offering superior carbon sequestration capabilities, enhanced durability, and improved overall performance.\|[0065] The preferred embodiment of the present invention addresses the limitations of previous approaches by utilizing brown algae species, particularly “Macrocystis pyrifera”, which have evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions. This makes them significantly more effective for CO2 absorption compared to red and green algae species. The use of brown algae provides a more efficient and targeted approach to carbon sequestration in concrete, leveraging their natural adaptations to marine environments.\|[0066] A critical innovation in the preferred embodiment is the formation of alginate beads using brown algae powder through a process called ionic gelation. This process dramatically increases the surface area available for CO2 absorption, enhancing it by orders of magnitude compared to simply mixing algae powder into the concrete. The alginate beads form a matrix across the surface of the concrete, which significantly enhances long-term sequestration and improves the concrete's durability. This matrix structure allows for more uniform and efficient carbon dioxide capture throughout the concrete, leading to superior performance over extended periods.\|[0067] The formation of alginate beads offers several key advantages over traditional methods. The increased surface area provided by the beads allows for more efficient CO2 absorption, while also promoting the formation of more stable calcium carbonate. This stability is crucial for long-term carbon sequestration, ensuring that the captured CO2 remains locked within the concrete structure for extended periods. Additionally, the uniform distribution of alginate beads throughout the concrete mix ensures that the CO2 capture potential is evenly spread, maximizing the overall sequestration capacity of the concrete.\|[0068] The alginate beads in the preferred embodiment interact synergistically with other components of the concrete mix, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance the overall performance and carbon sequestration capabilities of the concrete. For instance, the presence of alginate beads leads to enhanced pozzolanic reactions with fly ash, creating more sites within the concrete composition for capturing carbon dioxide. This increased reactivity not only improves the concrete's strength but also its ability to absorb CO2 over time.\|[0069] In the case of GGBFS, the alginate beads increase both the hydration and carbonation processes, effectively prolonging the period during which the concrete can absorb carbon dioxide. This extended absorption window is crucial for maximizing the total amount of CO2 sequestered over the lifetime of the concrete structure. Similarly, the interaction between alginate beads and metakaolin results in increased pozzolanic activity, further enhancing the concrete's performance and carbon capture capabilities.\|[0070] The alginate beads also enhance the CO2 sequestration capabilities of other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4). The beads create localized high-moisture environments that facilitate the dissolution of these minerals, leading to increased formation of carbonate compounds. This synergistic effect amplifies the overall carbon sequestration potential of the concrete, making it significantly more effective at reducing atmospheric CO2 levels compared to traditional concrete formulations.\|[0071] One of the most crucial roles played by the alginate beads in the preferred embodiment is in moisture retention, which is essential for the carbon sequestration process. The beads absorb and retain water, creating localized high-humidity environments within the concrete matrix. This increased moisture content is vital for facilitating greater direct air capture (DAC) of CO2, as the carbonation process reacts more readily in the presence of water. The absorbed water acts as a medium in which CO2 can dissolve, forming carbonic acid (H2CO3) and initiating a series of chemical reactions that lead to carbon sequestration.\|[0072] The presence of moisture within the alginate beads creates conditions favorable for the formation of bicarbonate (HCO3-) ions. This process is fundamental to the sequestration of various compounds within the concrete matrix. As CO2 dissolves and forms carbonic acid, it interacts with the calcium ions present within the alginate beads. This interaction leads to the formation of stable calcium carbonate, effectively locking the captured CO2 into the concrete structure. This process not only increases the overall CO2 uptake but also contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability.\|[0073] The formation of bicarbonate (HCO3-) ions in the presence of moisture from alginate beads is a crucial process in the carbon sequestration mechanism of the concrete. The alginate beads, which are rich in carboxyl groups, absorb and retain water, creating localized high-humidity environments within the concrete matrix. As atmospheric CO2 dissolves in this water, it forms carbonic acid (H2CO3). In the presence of moisture, the carboxyl groups in the alginate react with this carbonic acid, leading to the formation of bicarbonate (HCO3-) ions.\|[0074] This process is critical in accordance with the preferred embodiment because the bicarbonate ions serve as an intermediate step in the overall carbon mineralization process. The bicarbonate ions can further react with calcium ions within the alginate beads or from other sources in the concrete to form stable calcium carbonate (CaCO3). This reaction sequence effectively locks in the absorbed CO2, converting it from a gaseous form to a solid, stable mineral form within the concrete structure. The continuous moisture provision by the alginate beads ensures that this bicarbonate formation process can occur over an extended period, prolonging the concrete's carbon capture capabilities. This ongoing process contributes to the concrete's ability to sequester CO2 not only during the initial curing phase but also throughout its service life, albeit at a slower rate in later stages.\|[0075] An embodiment of the present invention comprises a carbon-sequestering concrete composition with specific components and their respective percentages by mass. Alternative embodiments deviate slightly from the specific percentages by mass presented in the foregoing.\|[0076] The composition includes Fly Ash (Class F) at 25%, which serves as the primary binder and significantly reduces CO2 emissions compared to traditional cement. This component allows for increased CO2-reactive materials in the mixture, enhancing the overall carbon sequestration potential of the concrete.\|[0077] Ground Granulated Blast Furnace Slag (GGBFS) constitutes 20% of the mixture. This component enhances the strength and durability of the concrete while acting as a supplementary binder. The inclusion of GGBFS contributes to the reduction of the carbon footprint associated with concrete production by partially replacing traditional cement.\|[0078] Metakaolin, comprising 5% of the mixture, improves early strength and reduces permeability of the concrete. This component allows room for more CO2 capture materials, further enhancing the carbon sequestration capabilities of the concrete. The inclusion of metakaolin also contributes to the overall sustainability of the mixture by reducing the need for energy-intensive cement production.\|[0079] Recycled Aggregates make up 20% of the composition, while Natural Aggregates constitute 15%. The use of recycled aggregates significantly reduces the environmental impact of the concrete production process by minimizing the need for new raw materials extraction. Natural aggregates provide the necessary mechanical strength to the concrete. The balance between recycled and natural aggregates is carefully optimized to maintain the structural integrity of the concrete while maximizing its sustainability.\|[0080] Silica Fume, at 2% of the mixture, fills micro-pores and enhances the strength and durability of the concrete. This component improves the overall pore structure of the concrete, which is crucial for both strength development and carbon sequestration potential. The fine particles of silica fume react with calcium hydroxide produced during cement hydration, forming additional calcium silicate hydrate (C—S—H) gel, which enhances the concrete's properties.\|[0081] Sodium Hydroxide (NaOH) and Sodium Silicate (Na2SiO3) serve as activators for the geopolymerization process, constituting 1.5% and 2.5% of the mixture respectively. These components are essential for activating the aluminosilicate materials in the mixture, particularly the fly ash and GGBFS. The careful balance of these activators ensures optimal reaction efficiency while minimizing environmental impact.\|[0082] Algae Biomass, used for creating alginate beads, makes up 2% of the mixture. This component is crucial for maximizing CO2 sequestration potential through the formation of alginate beads and direct air capture. The algae biomass is transformed into alginate beads through a process called ionic gelation, which dramatically increases the surface area available for CO2 absorption.\|[0083] Calcium Carbonate (CaCO3) and Magnesium Carbonate (MgCO3) each constitute 2% of the mixture. These components enhance carbonation during curing and beyond, improving overall CO2 capture. They react with CO2 to form stable carbonate compounds, effectively sequestering carbon within the concrete structure.\|[0084] Silica from Algae, comprising 1% of the mixture, serves as a sustainable silica source that improves strength with minimal environmental impact. This component contributes to the overall sustainability of the concrete mixture while enhancing its mechanical properties.\|[0085] Magnesium Silicate and Olivine (finely ground) each make up 1% of the mixture. These components enhance CO2 sequestration through mineral carbonation. The fine grinding of olivine increases its surface area, making it more reactive and efficient in capturing CO2. These materials react with atmospheric CO2 to form stable carbonate minerals, effectively locking away carbon for long periods.\|[0086] Basalt Rock Dust, constituting 1% of the mixture, provides trace minerals and enhances CO2 uptake through mineral carbonation. This component contributes to the overall carbon sequestration potential of the concrete while also improving its mechanical properties.\|[0087] Biochar (Activated) makes up 1% of the mixture. This component sequesters carbon and improves internal curing of the concrete. Biochar's porous structure allows it to absorb and retain CO2, contributing significantly to the overall carbon sequestration capabilities of the concrete.\|[0088] Alginate Beads, maximized at 1.5% of the mixture, play a crucial role in enhancing CO2 capture. These beads, formed through ionic gelation of brown algae powder, dramatically increase the surface area available for CO2 absorption. They form a matrix across the concrete surface, significantly enhancing long-term sequestration and improving durability.\|[0089] Carbonation Accelerators (C—S—H Seeds) constitute 1.5% of the mixture. These accelerate strength gain and CO2 uptake during curing. The C—S—H seeds provide nucleation sites for the formation of additional calcium silicate hydrate gel, which not only enhances the concrete's strength but also increases its capacity to absorb CO2.\|[0090] Water, making up 1% of the mixture, is necessary for workability and chemical reactions. The water content is carefully controlled to ensure optimal hydration of cementitious materials and proper workability of the concrete mix, while also facilitating the various chemical reactions involved in CO2 sequestration.\|[0091] This embodiment of the carbon-sequestering concrete composition demonstrates superior carbon sequestration capabilities compared to conventional concrete. For every 1,000 tons of concrete produced, this embodiment emits 81.4 tons of CO2 but sequesters 91.25 tons of CO2, resulting in a net sequestration of 9.85 tons of CO2. This represents a total reduction of 909.85 tons of CO2 per 1,000 tons produced, or a 101.1% reduction compared to conventional concrete.\|[0092] The CO2 sequestration in this embodiment occurs through several mechanisms, including biochar absorption, algae biomass uptake, carbonates reaction, mineral carbonation, alginate bead absorption, and CO2 absorption during curing. The total CO2 sequestered amounts to 91,250 kg (91.25 tonnes) per 1,000 tons of concrete produced.\|[0093] The carbon-sequestering concrete composition described in this embodiment demonstrates remarkable carbon sequestration capabilities that significantly outperform conventional concrete. For every 1,000 tons of concrete produced, this innovative composition achieves a net carbon sequestration of 9.85 tons of CO2, in stark contrast to conventional concrete which emits approximately 900 tons of CO2 for the same amount produced. This results in a total reduction of 909.85 tons of CO2 per 1,000 tons produced, representing a 101.1% reduction compared to conventional concrete.\|[0094] The superior carbon sequestration performance of this concrete composition is achieved through a combination of reduced emissions during production and active carbon capture mechanisms. While the embodiment emits 81.4 tons of CO2 during production, it sequesters 91.25 tons of CO2, resulting in the net negative carbon footprint. This remarkable feat is accomplished through several key mechanisms that work synergistically to capture and store carbon dioxide.\|[0095] The CO2 sequestration in this embodiment occurs through several primary mechanisms, including the following: Biochar absorption, which accounts for 29,333 kg of CO2 sequestered. The activated biochar in the mixture acts as a highly effective carbon sink due to its porous structure and high surface area. Algae Biomass uptake, responsible for sequestering 36,667 kg of CO2. The algae biomass, particularly when transformed into alginate beads, provides a substantial contribution to the overall carbon capture capacity of the concrete. Carbonates Reaction, which sequesters 2,000 kg of CO2. This involves the reaction of CO2 with calcium and magnesium carbonates present in the mixture, forming stable carbonate compounds. Mineral Carbonation, accounting for 2,500 kg of CO2 sequestered. This process involves the reaction of CO2 with minerals such as magnesium silicate and olivine to form stable carbonate minerals. Alginate Beads, which directly capture 750 kg of CO2 but also play a crucial role in enhancing the capture efficiency of other materials. The alginate beads, formed through ionic gelation of brown algae powder, create a matrix across the concrete surface that significantly increases the surface area available for CO2 absorption. CO2 absorbed during curing, which accounts for 20,000 kg of the total CO2 sequestered. This substantial amount is captured during the initial setting and hardening phase of the concrete.\|[0096] These mechanisms in an embodiment collectively result in a total CO2 sequestration of 91,250 kg (91.25 tonnes) per 1,000 tons of concrete produced. The synergistic interactions between the various components, particularly the alginate beads and other concrete constituents like geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS), enhance pozzolanic reactions and create additional sites for carbon dioxide capture. Furthermore, the moisture retention properties of the alginate beads create localized high-humidity environments within the concrete, facilitating greater direct air capture of CO2 throughout the concrete's service life.\|[0097] This innovative concrete composition not only addresses the carbon emissions associated with concrete production but also actively removes CO2 from the atmosphere, representing a significant advancement in sustainable construction materials.\|[0098] This embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0099] The alginate beads, formed through ionic gelation of brown algae powder, play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0100] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0101] By incorporating these innovative features, this embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0102] An alternative embodiment of the present invention comprises a carbon-sequestering concrete composition with the following components and their respective percentages by mass\| - Fly Ash (Class F): 22%\| - Ground Granulated Blast Furnace Slag (GGBFS): 20%\| - Metakaolin: 4%\| - Recycled Aggregates: 20%\| - Natural Aggregates: 12%\| - Silica Fume: 3%\| - Sodium Hydroxide (NaOH): 1%\| - Sodium Silicate (Na2SiO3): 2%\| - Algae Biomass (for Beads): 3%\| - Calcium Carbonate (CaCO3): 3%\| - Magnesium Carbonate (MgCO3): 3%\| - Silica from Algae: 1%\| - Magnesium Silicate: 2%\| - Olivine (Finely Ground): 3%\| - Basalt Rock Dust: 2%\| - Biochar (Activated): 2%\| - Alginate Beads (Maximized): 3%\| - Carbonation Accelerators (C—S—H Seeds): 2%\| - Water: 1%\|[0122] In this alternative embodiment, the Fly Ash (Class F) content is reduced to 22% in such embodiment to allow for increased CO2-reactive materials. This adjustment maintains the primary binding function while enhancing the overall carbon sequestration potential of the concrete. The Ground Granulated Blast Furnace Slag (GGBFS) in such embodiment is included at 20%, continuing to enhance strength and durability while acting as a supplementary binder. This component contributes significantly to reducing the carbon footprint associated with concrete production. Metakaolin is reduced to 4% in such embodiment, still improving early strength and reducing permeability while allowing for more CO2 capture materials. This adjustment contributes to the overall sustainability of the mixture. The ratio of Recycled Aggregates to Natural Aggregates is adjusted to 20% and 12% respectively in accordance with such embodiment. This change further reduces the environmental impact of the concrete production process while maintaining necessary mechanical strength. Silica Fume is increased to 3% to enhance the pore structure, strength, and durability of the concrete. This increase improves the overall performance and CO2 sequestration potential. The activators, Sodium Hydroxide (NaOH) and Sodium Silicate (Na2SiO3), are adjusted to 1% and 2% respectively. This optimization balances the geopolymerization process while minimizing environmental impact. Algae Biomass for beads is increased to 3%, maximizing CO2 sequestration potential through enhanced alginate bead formation and direct air capture. Both Calcium Carbonate (CaCO3) and Magnesium Carbonate (MgCO3) are increased to 3% each in accordance with this embodiment, enhancing carbonation during curing and beyond, thus improving overall CO2 capture. Magnesium Silicate is increased to 2%, and Olivine (Finely Ground) to 3%, enhancing CO2 sequestration through increased mineral carbonation potential. Basalt Rock Dust is increased to 2%, providing more trace minerals and enhancing CO2 uptake through mineral carbonation. Biochar (Activated) is increased to 2%, improving carbon sequestration and internal curing of the concrete. Alginate Beads are included at 3% in accordance with such embodiment, significantly enhancing CO2 capture and improving the concrete's overall performance. Carbonation Accelerators (C—S—H Seeds) are increased to 2%, further accelerating strength gain and CO2 uptake during curing. Water content remains at 1%, maintaining the necessary workability and facilitating chemical reactions.\|[0123] This alternative embodiment demonstrates enhanced carbon sequestration capabilities. For every 1,000 tons of concrete produced, this embodiment creates approximately 64.2 tons of CO2 but sequesters 101 tons of CO2 through direct air capture (DAC) and mineralization. This results in a net sequestration of approximately 36.8 tons of CO2 per 1,000 tons of concrete produced in accordance with an exemplary implementation.\|[0124] The carbon sequestration in this embodiment occurs through several mechanisms, including biochar absorption, algae biomass uptake, carbonates reaction, mineral carbonation, alginate bead absorption, and CO2 absorption during curing. The total CO2 sequestered amounts to 101,000 kg (101 tonnes) per 1,000 tons of concrete produced.\|[0125] This embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0126] The alginate beads, formed through ionic gelation of brown algae powder, play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0127] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability in an embodiment. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0128] By incorporating these innovative features and optimizing the component ratios, this alternative embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0129] The carbon-sequestering concrete composition described in the embodiments of the invention in an example is designed to maximize eligibility for significant tax credits and incentives, potentially resulting in substantial cost savings for concrete producers and users. In an example, the tax credits could be allocated for 1,000 tons of concrete produced as an embodiment of the invention in accordance with the following:\|[0130] Section 45Q tax credits could provide approximately $100,000 to $150,000 in savings per 1,000 tons of concrete produced, depending on the final determination by the EPA/IRS and the results of a Life Cycle Assessment (LCA). This estimate is based on the net carbon sequestration capabilities of the concrete, which ranges from 9.85 to 36.8 tons of CO2 per 1,000 tons of concrete produced, depending on the specific embodiment.\|[0131] The Investment Tax Credit could cover up to 30% of a concrete mixer's investment in this carbon-sequestering concrete technology. This credit would apply to the capital expenditures required to implement the new production methods and equipment necessary for manufacturing this innovative concrete.\|[0132] Additional tax incentives that may be applicable in association with and as an expected benefit of an embodiment of the invention include:\|[0133] R&D tax credits for the ongoing development and improvement of the carbon-sequestering concrete technology. Production Tax Credits for the manufacture of environmentally beneficial products. Various federal and state tax incentives designed to promote sustainable construction practices and materials.\|[0134] When considering a larger scale of production, for example 20 medium sized building construction projects, the total savings from these combined tax credits and incentives could exceed $5 million for a concrete producer. This estimate takes into account the cumulative effect of the various tax benefits across multiple projects.\|[0135] The economic benefits of these tax credits extend beyond mere cost savings. They also enhance the competitiveness of the carbon-sequestering concrete in the market. Before applying any tax credits, the price of this innovative concrete is approximately $138 per ton, which is already competitive with conventional concrete. However, after factoring in the tax credits, the effective price drops to around $112 per ton, making it more economical than conventional concrete options.\|[0136] In accordance with various embodiments, the exact allocation and amount of tax credits may vary depending on factors such as the specific project details, the concrete producer's financial situation, and any changes in tax laws or regulations. Additionally, the realization of these tax benefits would likely require careful documentation of the carbon sequestration capabilities of the concrete, as well as compliance with relevant regulatory requirements, which is an intended use in accordance with an embodiment of the invention.\|[0137] Another embodiment of the invention comprises a carbon-sequestering concrete composition optimized for maximum CO2 sequestration and economic viability through tax incentives, as follows:\|[0138] The composition of this carbon-sequestering concrete in such embodiment is carefully formulated to maximize both CO2 sequestration capabilities and eligibility for tax credits. The mixture, designed for a 1,000-ton batch, comprises several key components that work synergistically to achieve these goals.\|[0139] Aluminosilicate materials form the foundation of the geopolymer binder system in such embodiment. These include 30% Fly Ash (Class F), 20% Ground Granulated Blast Furnace Slag (GGBFS), 5% Metakaolin, and 3% Silica Fume. These materials not only contribute to the strength and durability of the concrete but also play a crucial role in CO2 sequestration through pozzolanic reactions.\|[0140] A significant portion of the mix in such embodiment is dedicated to CO2-absorbing materials. This includes 15% Magnesium Silicate, 15% finely ground Olivine, 10% Activated Biochar, 3% Calcium Carbonate (CaCO3), and 2% Magnesium Carbonate (MgCO3). These components are specifically chosen for their high CO2 sequestration potential and their ability to form stable carbonate compounds over time.\|[0141] The aggregate portion of the mix consists of 10% Natural Aggregates and 5% Recycled Aggregates, balancing structural requirements with sustainability considerations in accordance with such embodiment. The alkaline activators, crucial for the geopolymerization process, include 2% Sodium Hydroxide (NaOH) and 4% Sodium Silicate (Na2SiO3).\|[0142] A key innovation in this embodiment is the incorporation of algae-derived components. This comprises 1% Silica from Algae, 3% Algae Biomass for bead formation, and 5% Alginate Beads. These components significantly enhance the CO2 sequestration capabilities of the concrete through increased surface area and the creation of localized high-humidity environments that facilitate CO2 absorption.\|[0143] The mixture in such embodiment also comprises 2% Carbonation Accelerators in the form of C—S—H Seeds, which enhance the rate of CO2 uptake during the curing process. The water content is maintained at 5%, with small amounts of superplasticizers (0.5%) and air-entraining agents (0.1%) added to optimize workability and durability.\|[0144] The production process of this concrete composition in such embodiment has been observed by the inventor to result in total emissions of 108,550 kg CO2 per 1,000 tons produced. However, the CO2 sequestration capabilities of the mixture are substantial, with a total CO2 sequestration potential of 435,000 kg CO2 per 1,000 tons of concrete. This results in a net negative carbon footprint of −326,450 kg CO2 per 1,000 tons of concrete produced in accordance with inventor observations.\|[0145] The CO2 sequestration occurs through several mechanisms in accordance with such embodiment. The Magnesium Silicate and Olivine each sequester 45,000 kg CO2. The Activated Biochar contributes significantly with 200,000 kg CO2 sequestered. The Algae Biomass and Alginate Beads together sequester 80,000 kg CO2. The Calcium and Magnesium Carbonates add another 5,000 kg CO2 to the total. Additionally, the CO2 curing process is estimated to sequester an additional 50,000 kg CO2.\|[0146] This embodiment is designed to maximize eligibility for tax credits, particularly the Section 45Q tax credit for carbon oxide sequestration. For every 1,000 tons of concrete produced, this composition is eligible for approximately $26,100 in Section 45Q tax credits. When combined with other available tax credits such as the Investment Tax Credit and R&D credits, the total tax credits per 1,000 tons could reach approximately $354,100 in accordance with the regulations in place as of September 2024.\|[0147] The economic viability of this concrete composition in such embodiment is further enhanced by these tax incentives. After accounting for all applicable tax credits, the effective cost of this concrete is estimated to be $57.85 per ton, making it highly competitive in the market.\|[0148] In comparison to other carbon-reducing concrete technologies, this embodiment demonstrates superior performance. For instance, when compared to Blue Planet's concrete, which sequesters 330 tons CO2 per 1,000 tons of concrete, this embodiment sequesters 435 tons CO2. This results in higher eligibility for Section 45Q tax credits and overall tax credits under applicable regulations in place in September 2024.\|[0149] The enhanced CO2 sequestration capabilities of this concrete composition in such embodiment are achieved through the synergistic interactions between its components, particularly the alginate beads and other concrete constituents like geopolymers, fly ash, and ground granulated blast furnace slag. These interactions enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The moisture retention properties of the alginate beads create localized high-humidity environments within the concrete, facilitating greater direct air capture of CO2 throughout the concrete's service life.\|[0150] This innovative concrete composition in accordance with such embodiment not only addresses the carbon emissions associated with concrete production but also actively removes CO2 from the atmosphere, representing a significant advancement in sustainable construction materials. Its superior carbon sequestration capabilities, combined with its economic viability through tax incentives, position it as a potentially disruptive technology in the concrete industry.\|[0151] The carbon-sequestering concrete composition described in the embodiment can be formulated with varying proportions of its key components to optimize performance and CO2 sequestration capabilities. The aluminosilicate materials, which form the foundation of the geopolymer binder system, can range from 30-60% of the total composition. This range allows for flexibility in adjusting the mix based on specific project requirements and material availability. The CO2-absorbing materials, crucial for the concrete's carbon sequestration properties, can constitute 30-50% of the mixture. This range ensures a significant portion of the concrete is dedicated to active CO2 absorption while maintaining structural integrity.\|[0152] The aggregate portion, balancing structural requirements with sustainability considerations, can range from 10-20% of the total composition in accordance with such embodiment. The alkaline activators, essential for the geopolymerization process, can comprise 5-10% of the mixture. The innovative algae-derived components, which significantly enhance CO2 sequestration capabilities, can make up 5-15% of the composition. This range allows for optimization of the algae-based materials' contribution to carbon capture. Carbonation accelerators can be included at 1-5% to enhance CO2 uptake during curing, while water content can be maintained between 4-6% to ensure proper workability and hydration.\|[0153] These ranges have been determined through extensive experimentation and observation by the inventor. They allow for the concrete composition in accordance with such embodiment to sequester at least 400 kg of CO2 per 1,000 kg of concrete produced, achieving a net negative carbon footprint of at least 300 kg CO2 per 1,000 kg of concrete. This flexibility in composition enables the concrete to be tailored for specific applications while maintaining its superior carbon sequestration capabilities and economic viability through tax incentives.\|[0154] The innovative features incorporated in the preferred embodiment address the limitations of previous approaches and provide a concrete composition with superior carbon sequestration capabilities. The use of brown algae-derived alginate beads, their synergistic interactions with other concrete components, and the enhanced moisture retention properties all contribute to a more effective and long-lasting carbon capture solution. This advanced concrete formulation not only reduces the carbon footprint associated with concrete production but also actively removes CO2 from the atmosphere throughout its service life, representing a significant step forward in sustainable construction materials.\|[0155] While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. It is not intended that the invention be limited by the specific examples provided within the specification. While the invention has been described with reference to the aforementioned specification, the descriptions and illustrations of the embodiments herein are not meant to be construed in a limiting sense. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. Furthermore, it shall be understood that all aspects of the invention are not limited to the specific depictions, configurations or relative proportions set forth herein which depend upon a variety of conditions and variables. It should be understood that various alternatives to the embodiments of the invention described herein may be employed in practicing the invention. It is therefore contemplated that the invention shall also cover any such alternatives, modifications, variations or equivalents. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby.	(US20250250199)\|CROSS REFERENCE TO RELATED APPLICATIONS\|[0001] This application claims the benefit of and incorporates by reference in its entirety U.S. Provisional Patent Application No. 63/469,108, filed May 26, 2023 which is incorporated herein by reference in its entirety. This application also claims the benefit of, is a continuation-in-part of, and incorporates by reference in its entirety U.S. patent application Ser. No. 18/722,678, filed on Jun. 21, 2024, and U.S. patent application Ser. No. 18/814,312 filed on Aug. 23, 2024. This application also claims the benefit of and incorporates by reference in its entirety International Patent Application No. PCT/US24/13913, filed Feb. 1, 2024.\|(US20250250199)\|FIELD OF THE INVENTION\|[0002] The present invention relates to the field of sustainable construction materials, specifically to carbon-sequestering concrete compositions and methods for their production.\|BACKGROUND OF THE INVENTION\|[0003] Concrete is one of the most widely used construction materials globally, with over 4 billion metric tons produced annually.\|[0004] However, conventional Portland cement concrete production is a significant contributor to global carbon dioxide emissions, accounting for 7-8% of all CO2 emissions worldwide. This represents an immense environmental burden, generating over 2 gigatons of carbon dioxide per year during cement production alone.\|[0005] Recent efforts to mitigate the carbon footprint of concrete have explored various approaches, including the incorporation of seawater and algae into concrete mixes to enable CO2 sequestration.\|[0006] However, these existing methods have achieved only modest and inconsistent levels of CO2 absorption that pale in comparison to the scale of emissions from concrete production.\|[0007] One such approach is described in Korean Patent No. 102079643 B1 to Lee et al. (“LEE”), which discloses a carbon dioxide-absorbing marine concrete composition made by mixing blast furnace slag, fly ash, metakaolin, sodium silicate, and dried algae powder. While this composition attempts to address the environmental impact of concrete production, it suffers from several significant limitations.\|[0008] The use of algae powder alone in the manner disclosed by LEE fails to fully leverage the carbon sequestration potential of marine algae, as it does not provide optimal surface area for CO2 absorption or create the necessary conditions for long-term carbon mineralization. Furthermore, simply mixing algae powder into concrete does not facilitate the formation of a matrix across the concrete surface that could enhance long-term sequestration and improve durability. There is a need for an innovative approach that can dramatically increase the CO2 absorption capacity of concrete, create synergistic interactions with other concrete components, and provide a mechanism for moisture retention to facilitate greater direct air capture of CO2. Such an approach would overcome the limitations of current algae-based concrete technologies and offer superior CO2 sequestration capabilities, enhanced durability, and improved overall performance.\|[0009] The need for carbon-capturing concrete has become increasingly urgent as the construction industry seeks to reduce its significant carbon footprint. To incentivize the adoption of such environmentally beneficial technologies, various tax credits and incentives have been established. Section 45Q of the Internal Revenue Code provides tax credits for carbon oxide sequestration, which can result in substantial savings for concrete producers utilizing this technology. Additionally, the Investment Tax Credit offers up to 30% credit on capital investments in carbon-capturing technologies. Other applicable incentives include R&D tax credits, Production Tax Credits, and various federal and state tax incentives designed to promote sustainable construction practices. These financial incentives not only make the adoption of carbon-sequestering concrete more economically viable but also align with broader policy goals of reducing greenhouse gas emissions and promoting sustainable development in the construction industry.\|[0010] These limitations result in a concrete composition that, while attempting to address environmental concerns, falls short of achieving significant and long-lasting carbon sequestration. The present invention seeks to overcome these limitations by providing a novel carbon-absorbing concrete composition and method of production that offers superior CO2 sequestration capabilities, enhanced durability, and improved overall performance compared to existing technologies.\|SUMMARY OF THE INVENTION\|[0011] The present invention relates to a carbon-sequestering concrete composition and method of production that addresses the limitations of previous approaches to reducing the carbon footprint of concrete.\|[0012] At the core of the preferred embodiment is the utilization of brown algae species, particularly “Macrocystis pyrifera”, which are transformed into alginate beads through a process called ionic gelation. These alginate beads dramatically increase the surface area available for CO2 absorption, forming a matrix across the concrete surface that enhances long-term sequestration and improves durability.\|[0013] The alginate beads are created through ionic gelation using brown algae powder. This process involves mixing the algae powder with water to create an alginate solution, which is then introduced dropwise into a bath containing calcium ions. As the droplets come into contact with the calcium ions, they undergo rapid gelation, forming stable, three-dimensional network structures with a high surface area, ideal for CO2 absorption and moisture retention in concrete.\|[0014] The preferred embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0015] The alginate beads play a crucial role in moisture retention in the context of the preferred embodiment, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0016] The preferred embodiment also addresses the formation of bicarbonate (HCO3-) ions in the presence of moisture from alginate beads, which is crucial for the carbon sequestration mechanism of the concrete. This process contributes to the concrete's ability to sequester CO2 not only during the initial curing phase but also throughout its service life.\|[0017] Furthermore, the alginate beads contribute to the self-healing of micro-cracks in the concrete, extending its lifespan and durability. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0018] In summary, the preferred embodiment provides a concrete composition with superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. It addresses the limitations of previous approaches and represents a significant advancement in sustainable construction materials.\|(US20250250199)\|BRIEF DESCRIPTION OF THE FIGURES\|[0019] FIG. 1 depicts the usage of an embodiment of the invention in association with a sidewalk.\|[0020] FIG. 2 depicts the usage of an embodiment of the invention in association with a pillar associated with a typical construction project.\|(US20250250199)\|DETAILED DESCRIPTION\|[0021] The preferred embodiment comprises a carbon-sequestering concrete and the associated methods of manufacture, addressing the limitations of previous methods and significantly enhancing CO2 absorption capabilities.\|[0022] At the core of this embodiment is the utilization of brown algae species, particularly “Macrocystis pyrifera”, which are transformed into alginate beads through a process called ionic gelation. These alginate beads dramatically increase the surface area available for CO2 absorption, forming a matrix across the concrete surface that enhances long-term sequestration and improves durability. The alginate beads in the preferred embodiment are created through a process called ionic gelation using brown algae powder, particularly from species “Macrocystis pyrifera”. This process is critical for enhancing CO2 absorption in the concrete mixture.\|[0023] The brown algae species “Macrocystis pyrifera” was chosen for creating alginate beads in the preferred embodiment due to its superior carbon sequestration capabilities. This species has evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions, making it significantly more effective for CO2 absorption compared to red and green algae species. The alginate extracted from Macrocystis pyrifera is particularly rich in carboxyl groups, which are crucial for the ionic gelation process used to form the beads. When mixed with water and introduced dropwise into a calcium ion bath, the alginate from Macrocystis pyrifera forms stable, three-dimensional network structures with a high surface area, ideal for CO2 absorption and moisture retention in concrete. In alternative embodiments, other brown algae species may serve as a substitute, including but not limited to Laminaria, Ascophyllum, Sargassum, and Fucus species. These alternative species also possess similar cell wall structures and carbon-binding capabilities, although Macrocystis pyrifera remains the preferred choice due to its particularly high alginate content and optimal gelation properties for concrete applications.\|[0024] To form the alginate beads, the brown algae powder is first mixed with water to create an alginate solution. This solution contains the alginate polymers naturally present in the cell walls of brown algae, which are rich in carboxyl groups.\|[0025] The alginate solution in an embodiment is then introduced dropwise into a bath containing divalent cations, typically calcium ions. As the alginate droplets come into contact with the calcium ions, they undergo a rapid gelation process. The calcium ions crosslink the alginate polymers, forming a stable, three-dimensional network structure. This ionic gelation process results in the formation of spherical alginate beads with a significantly increased surface area compared to the original algae powder. The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture. The ionic gelation process for forming alginate beads in an embodiment begins with mixing brown algae powder, particularly from species like “Macrocystis pyrifera”, with water to create an alginate solution. This solution contains the alginate polymers naturally present in the cell walls of brown algae, which are rich in carboxyl groups. The alginate solution is then introduced dropwise into a bath containing divalent cations, typically calcium ions. As the alginate droplets come into contact with the calcium ions, they undergo a rapid gelation process. The calcium ions crosslink the alginate polymers, forming a stable, three-dimensional network structure. This process results in the formation of spherical alginate beads with a significantly increased surface area compared to the original algae powder. The beads have a porous structure that allows for efficient CO2 absorption and retention of moisture. The size and density of the alginate beads can be controlled by adjusting various parameters during the gelation process, such as the concentration of the alginate solution, the type and concentration of the crosslinking ions, and the droplet size. This allows for optimization of the beads' properties to suit the specific requirements of the concrete mixture. Once formed, the alginate beads are collected and may undergo further processing, such as washing to remove excess ions and drying to a desired moisture content. The resulting beads are then ready to be incorporated into the concrete mixture, where they will play a crucial role in enhancing CO2 sequestration and improving the overall performance of the concrete in accordance with an embodiment of the invention.\|[0026] The size and density of the alginate beads can be controlled by adjusting various parameters during the gelation process, such as the concentration of the alginate solution, the type and concentration of the crosslinking ions, and the droplet size. This allows for optimization of the beads' properties to suit the specific requirements of the concrete mixture.\|[0027] Once formed, the alginate beads are collected and may undergo further processing, such as washing to remove excess ions and drying to a desired moisture content. The resulting beads are then ready to be incorporated into the concrete mixture, where they will play a crucial role in enhancing CO2 sequestration and improving the overall performance of the concrete.\|[0028] The formation of these alginate beads through ionic gelation is a key innovation that sets the preferred embodiment of the invention apart from previous approaches that simply mixed algae powder into concrete. The beads provide a matrix across the surface of the concrete, dramatically enhancing long-term sequestration and improving the concrete's durability.\|[0029] The alginate beads formed from brown algae powder significantly increase the CO2 absorption surface area compared to simply using algae powder in concrete. This enhancement in surface area is achieved through the ionic gelation process, which creates a porous, three-dimensional structure within each bead.\|[0030] When algae powder is directly mixed into concrete in accordance with the preferred embodiment, it remains as discrete particles with limited surface area exposed for CO2 interaction. In contrast, the alginate beads form a matrix across the surface of the concrete, dramatically increasing the total surface area available for carbon dioxide absorption.\|[0031] The ionic gelation process creates a network of interconnected pores within each alginate bead. This porous structure allows CO2 molecules to penetrate deep into the bead, rather than just interacting with the outer surface. As a result, the effective surface area for CO2 absorption is multiplied many times over compared to solid algae powder particles in accordance with the preferred embodiment.\|[0032] Furthermore, the alginate beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. This moisture retention further enhances CO2 absorption, as the carbonation process reacts more readily in the presence of water. The combination of increased surface area and moisture retention allows for significantly more efficient CO2 capture and conversion to stable carbonate compounds.\|[0033] The size and density of the alginate beads can be controlled during the gelation process in accordance with various embodiments, allowing for optimization of the surface area to volume ratio. By adjusting parameters such as alginate concentration, crosslinking ion type and concentration, and droplet size, the beads can be tailored to maximize their CO2 absorption capacity.\|[0034] Additionally, the alginate beads create a more uniform distribution of CO2 absorption sites throughout the concrete matrix compared to algae powder. This even distribution ensures that the carbon sequestration potential is maximized across the entire concrete structure, rather than being limited to localized areas where algae powder particles might cluster.\|[0035] The cumulative effect of these factors in accordance with the preferred embodiment-increased surface area, porous structure, moisture retention, and uniform distribution-results in CO2 absorption capabilities that are orders of magnitude greater than what can be achieved with simple algae powder incorporation associated with other attempts. This dramatic enhancement in carbon sequestration efficiency is a critical innovation of the preferred embodiment of the invention, enabling concrete structures to serve as highly effective carbon sinks throughout their service life.\|[0036] The preferred embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS).\|[0037] These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption. The alginate beads also play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2.\|[0038] The preferred embodiment enhances pozzolanic reactions through the synergistic interaction between alginate beads and various components of the concrete mix, particularly fly ash and metakaolin.\|[0039] Pozzolanic reactions occur when siliceous or aluminosiliceous materials react with calcium hydroxide in the presence of water to form compounds with cementitious properties. In the context of this invention, the alginate beads create localized high-humidity environments within the concrete matrix, which facilitates these reactions. The increased moisture content provided by the beads promotes the dissolution of silica and alumina from the pozzolanic materials, allowing them to react more readily with calcium hydroxide produced during the hydration of cement or geopolymer precursors. This enhanced reactivity leads to the formation of additional calcium silicate hydrate (C—S—H) and calcium aluminate hydrate (C-A-H) gels, which contribute to the concrete's strength and durability. Furthermore, the pozzolanic reactions consume calcium hydroxide, reducing the concrete's susceptibility to chemical attacks and improving its long-term performance. The increased pozzolanic activity also creates more sites for carbon dioxide capture within the concrete composition, as the newly formed C—S—H and C-A-H gels provide additional surface area for CO2 absorption and carbonation.\|[0040] The preferred embodiment creates additional sites for carbon dioxide capture through several mechanisms. The alginate beads formed from brown algae powder increase the surface area available for CO2 absorption, creating a matrix across the concrete surface that enhances long-term sequestration. This matrix structure provides numerous additional sites for CO2 to interact with and be captured by the concrete. Furthermore, the synergistic interactions between the alginate beads and other concrete components, such as fly ash and ground granulated blast furnace slag (GGBFS), lead to enhanced pozzolanic reactions in association with the preferred embodiment.\|[0041] These reactions create more sites in the concrete composition specifically for capturing carbon dioxide. The increased pozzolanic activity results in the formation of additional calcium silicate hydrate (C—S—H) and calcium aluminate hydrate (C-A-H) gels, which provide extra surface area for CO2 absorption and carbonation. The alginate beads also interact positively with other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4).\|[0042] The alginate beads in the preferred embodiment interact synergistically with additives like magnesium carbonate and olivine (Mg2SiO4) to enhance the concrete's CO2 sequestration capabilities. The moisture retention properties of the alginate beads play a crucial role in facilitating these interactions.\|[0043] For magnesium carbonate, the localized high-humidity environments created by the alginate beads promote its gradual dissolution within the concrete matrix. This dissolution process releases magnesium ions, which can then react with dissolved CO2 to form stable magnesium carbonate compounds, effectively capturing and storing atmospheric carbon dioxide.\|[0044] In the case of olivine (Mg2SiO4), the humidity retained by the alginate beads creates conditions favorable for its dissolution in accordance with the preferred embodiment. As the olivine dissolves, it releases magnesium ions into the concrete matrix. These magnesium ions can then interact with the alginate structure, enhancing the formation of magnesium carbonates. This process not only contributes to additional CO2 sequestration but also improves the overall strength and durability of the concrete.\|[0045] The alginate beads create “localized high-humidity environments” within the concrete through their unique moisture absorption and retention properties. When incorporated into the concrete mixture, these beads absorb and hold water, acting as microscopic reservoirs distributed throughout the concrete matrix.\|[0046] In accordance with the preferred embodiment, as the concrete cures and ages, the alginate beads continue to retain this moisture, creating small pockets of high humidity surrounding each bead. These localized high-humidity environments are crucial for facilitating CO2 absorption, as the carbonation process reacts more readily in the presence of water. The retained moisture provides a medium for atmospheric CO2 to dissolve, forming carbonic acid which then interacts with calcium ions to produce stable calcium carbonate. This process of CO2 absorption and carbonate formation is significantly enhanced by the consistent availability of moisture provided by the alginate beads, allowing for continuous carbon sequestration throughout the concrete's service life. Furthermore, these high-humidity microenvironments promote the gradual dissolution of other additives like magnesium carbonate and olivine, further enhancing the concrete's overall CO2 absorption capacity.\|[0047] The continuous moisture provision by the alginate beads ensures that these reactions can occur over an extended period, prolonging the concrete's carbon capture capabilities. As atmospheric CO2 dissolves in the water retained by the beads, it forms carbonic acid, which then reacts with the magnesium ions released from both magnesium carbonate and olivine to produce stable carbonate compounds. These interactions between the alginate beads and additives like magnesium carbonate and olivine create a self-sustaining cycle of CO2 absorption and mineralization within the concrete. The process continues throughout the concrete's service life, significantly enhancing its long-term carbon sequestration potential compared to traditional concrete compositions.\|[0048] The preferred embodiment prolongs the period of CO2 absorption through several innovative mechanisms. The alginate beads formed from brown algae powder play a crucial role in extending the carbon sequestration capabilities of the concrete over time. These beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix that facilitate ongoing CO2 absorption.\|[0049] The synergistic interactions between the alginate beads and other concrete components, such as ground granulated blast furnace slag (GGBFS), increase both the hydration and carbonation processes. This effectively extends the duration during which the concrete can actively absorb carbon dioxide from the atmosphere.\|[0050] Furthermore, the alginate beads enhance the CO2 sequestration capabilities of other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4). The humidity retained by the beads creates conditions that promote the gradual dissolution of these minerals, leading to sustained carbon capture over an extended period. The continuous process of CO2 absorption is supported by the ongoing formation of carbonate compounds within the concrete matrix.\|[0051] The alginate beads facilitate the dissolution of minerals including olivine (Mg2SiO4) to enhance carbon capture through several mechanisms. The beads absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. This increased moisture content promotes the gradual dissolution of olivine, releasing magnesium ions into the surrounding concrete. The humidity in the alginate beads creates these localized high moisture environments, which are crucial for facilitating olivine dissolution. As the olivine dissolves, the released magnesium ions interact with the alginate structure, enhancing the formation of magnesium carbonates. This process not only contributes to additional CO2 sequestration but also improves the overall strength and durability of the concrete. The continuous moisture provision by the alginate beads ensures that these reactions can occur over an extended period, prolonging the concrete's carbon capture capabilities. Furthermore, the beads provide additional surface area for basalt dissolution, which leads to further carbon capture. This synergistic interaction between the alginate beads and olivine creates a self-sustaining cycle of CO2 absorption and mineralization within the concrete, significantly enhancing its long-term carbon sequestration potential compared to traditional concrete compositions.\|[0052] As atmospheric CO2 dissolves in the water retained by the alginate beads, it forms carbonic acid, which then reacts with calcium ions to produce stable calcium carbonate. This cycle of absorption and mineralization continues throughout the concrete's service life, significantly prolonging its CO2 sequestration capabilities.\|[0053] Additionally, the formation of stable calcium carbonate contributes to the self-healing of micro-cracks in the concrete. This self-healing property not only extends the overall lifespan of the concrete but also maintains its ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure. The alginate beads also contribute to the self-healing of micro-cracks in the concrete through several mechanisms. As the concrete cures and ages, the alginate beads continue to absorb and retain moisture, creating localized high-humidity environments within the concrete matrix. When micro-cracks form, these moist environments facilitate the ongoing formation of carbonate compounds. As atmospheric CO2 dissolves in the water retained by the alginate beads, it forms carbonic acid, which then reacts with calcium ions to produce stable calcium carbonate. This calcium carbonate precipitates within the micro-cracks, gradually filling them and restoring the concrete's integrity. The continuous nature of this process, enabled by the moisture-retaining properties of the alginate beads, allows for ongoing self-healing throughout the concrete's service life. Additionally, the alginate beads' ability to enhance pozzolanic reactions and create additional sites for carbon dioxide capture contributes to the formation of supplementary binding materials that can further aid in crack repair. This self-healing property not only extends the overall lifespan of the concrete but also maintains its ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0054] By incorporating these innovative features, the preferred embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0055] The humidity retained by the alginate beads creates localized high moisture environments that facilitate the dissolution of these minerals, leading to further carbon capture opportunities. This process increases the overall number of sites available for CO2 sequestration within the concrete matrix. Lastly, the moisture retention properties of the alginate beads create conditions favorable for the ongoing formation of carbonate compounds throughout the concrete.\|[0056] As CO2 dissolves in the water absorbed by the beads, it forms carbonic acid, which then interacts with calcium ions to form stable calcium carbonate. This continuous process effectively creates new sites for carbon dioxide capture as the concrete ages, prolonging its CO2 sequestration capabilities over time.\|[0057] This innovative concrete composition not only reduces the carbon footprint associated with production but also actively removes CO2 from the atmosphere throughout its service life. The carbon capture process in the preferred embodiment occurs strongly over the initial approximately 60 days due to the rapid initial reactions between the alginate beads and atmospheric CO2, but continues on a smaller scale for many years thereafter.\|[0058] This prolonged sequestration is enabled by several key mechanisms:\|[0059] During the initial curing period, the alginate beads formed through ionic gelation provide a large surface area for CO2 absorption, allowing for rapid carbonation reactions. The beads absorb and retain moisture, creating localized high-humidity environments that facilitate the dissolution of CO2 and its reaction with calcium ions to form stable calcium carbonate.\|[0060] As the concrete continues to age, the synergistic interactions between the alginate beads and other components of the mix, such as ground granulated blast furnace slag (GGBFS) and fly ash, sustain the carbon capture process. These interactions lead to ongoing pozzolanic reactions and the creation of additional sites for CO2 absorption, albeit at a slower rate than during the initial curing period.\|[0061] The moisture retention properties of the alginate beads play a crucial role in maintaining conditions favorable for long-term CO2 sequestration. Even as the concrete ages, the beads continue to absorb and retain water from the environment, providing a medium for CO2 to dissolve and react with available calcium ions.\|[0062] Furthermore, the formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete. This self-healing process not only extends the lifespan of the concrete but also maintains pathways for continued CO2 absorption over many years.\|[0063] The gradual dissolution of minerals such as magnesium carbonate and olivine, facilitated by the moisture retained in the alginate beads, provides a slow but steady source of reactive components for ongoing CO2 sequestration. This process continues at a reduced rate long after the initial curing period, allowing the concrete to capture carbon dioxide from the atmosphere throughout its service life.\|[0064] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions in the alginate beads contributes to the self-healing of micro-cracks, further extending the concrete's lifespan and durability. By addressing the limitations of previous approaches, this invention represents a significant advancement in sustainable construction materials, offering superior carbon sequestration capabilities, enhanced durability, and improved overall performance.\|[0065] The preferred embodiment of the present invention addresses the limitations of previous approaches by utilizing brown algae species, particularly “Macrocystis pyrifera”, which have evolved robust cell walls with concentrated salts and carbon-binding structures optimized for ocean conditions. This makes them significantly more effective for CO2 absorption compared to red and green algae species. The use of brown algae provides a more efficient and targeted approach to carbon sequestration in concrete, leveraging their natural adaptations to marine environments.\|[0066] A critical innovation in the preferred embodiment is the formation of alginate beads using brown algae powder through a process called ionic gelation. This process dramatically increases the surface area available for CO2 absorption, enhancing it by orders of magnitude compared to simply mixing algae powder into the concrete. The alginate beads form a matrix across the surface of the concrete, which significantly enhances long-term sequestration and improves the concrete's durability. This matrix structure allows for more uniform and efficient carbon dioxide capture throughout the concrete, leading to superior performance over extended periods.\|[0067] The formation of alginate beads offers several key advantages over traditional methods. The increased surface area provided by the beads allows for more efficient CO2 absorption, while also promoting the formation of more stable calcium carbonate. This stability is crucial for long-term carbon sequestration, ensuring that the captured CO2 remains locked within the concrete structure for extended periods. Additionally, the uniform distribution of alginate beads throughout the concrete mix ensures that the CO2 capture potential is evenly spread, maximizing the overall sequestration capacity of the concrete.\|[0068] The alginate beads in the preferred embodiment interact synergistically with other components of the concrete mix, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance the overall performance and carbon sequestration capabilities of the concrete. For instance, the presence of alginate beads leads to enhanced pozzolanic reactions with fly ash, creating more sites within the concrete composition for capturing carbon dioxide. This increased reactivity not only improves the concrete's strength but also its ability to absorb CO2 over time.\|[0069] In the case of GGBFS, the alginate beads increase both the hydration and carbonation processes, effectively prolonging the period during which the concrete can absorb carbon dioxide. This extended absorption window is crucial for maximizing the total amount of CO2 sequestered over the lifetime of the concrete structure. Similarly, the interaction between alginate beads and metakaolin results in increased pozzolanic activity, further enhancing the concrete's performance and carbon capture capabilities.\|[0070] The alginate beads also enhance the CO2 sequestration capabilities of other additives in the mix, such as magnesium carbonate and olivine (Mg2SiO4). The beads create localized high-moisture environments that facilitate the dissolution of these minerals, leading to increased formation of carbonate compounds. This synergistic effect amplifies the overall carbon sequestration potential of the concrete, making it significantly more effective at reducing atmospheric CO2 levels compared to traditional concrete formulations.\|[0071] One of the most crucial roles played by the alginate beads in the preferred embodiment is in moisture retention, which is essential for the carbon sequestration process. The beads absorb and retain water, creating localized high-humidity environments within the concrete matrix. This increased moisture content is vital for facilitating greater direct air capture (DAC) of CO2, as the carbonation process reacts more readily in the presence of water. The absorbed water acts as a medium in which CO2 can dissolve, forming carbonic acid (H2CO3) and initiating a series of chemical reactions that lead to carbon sequestration.\|[0072] The presence of moisture within the alginate beads creates conditions favorable for the formation of bicarbonate (HCO3-) ions. This process is fundamental to the sequestration of various compounds within the concrete matrix. As CO2 dissolves and forms carbonic acid, it interacts with the calcium ions present within the alginate beads. This interaction leads to the formation of stable calcium carbonate, effectively locking the captured CO2 into the concrete structure. This process not only increases the overall CO2 uptake but also contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability.\|[0073] The formation of bicarbonate (HCO3-) ions in the presence of moisture from alginate beads is a crucial process in the carbon sequestration mechanism of the concrete. The alginate beads, which are rich in carboxyl groups, absorb and retain water, creating localized high-humidity environments within the concrete matrix. As atmospheric CO2 dissolves in this water, it forms carbonic acid (H2CO3). In the presence of moisture, the carboxyl groups in the alginate react with this carbonic acid, leading to the formation of bicarbonate (HCO3-) ions.\|[0074] This process is critical in accordance with the preferred embodiment because the bicarbonate ions serve as an intermediate step in the overall carbon mineralization process. The bicarbonate ions can further react with calcium ions within the alginate beads or from other sources in the concrete to form stable calcium carbonate (CaCO3). This reaction sequence effectively locks in the absorbed CO2, converting it from a gaseous form to a solid, stable mineral form within the concrete structure. The continuous moisture provision by the alginate beads ensures that this bicarbonate formation process can occur over an extended period, prolonging the concrete's carbon capture capabilities. This ongoing process contributes to the concrete's ability to sequester CO2 not only during the initial curing phase but also throughout its service life, albeit at a slower rate in later stages.\|[0075] An embodiment of the present invention comprises a carbon-sequestering concrete composition with specific components and their respective percentages by mass. Alternative embodiments deviate slightly from the specific percentages by mass presented in the foregoing.\|[0076] The composition includes Fly Ash (Class F) at 25%, which serves as the primary binder and significantly reduces CO2 emissions compared to traditional cement. This component allows for increased CO2-reactive materials in the mixture, enhancing the overall carbon sequestration potential of the concrete.\|[0077] Ground Granulated Blast Furnace Slag (GGBFS) constitutes 20% of the mixture. This component enhances the strength and durability of the concrete while acting as a supplementary binder. The inclusion of GGBFS contributes to the reduction of the carbon footprint associated with concrete production by partially replacing traditional cement.\|[0078] Metakaolin, comprising 5% of the mixture, improves early strength and reduces permeability of the concrete. This component allows room for more CO2 capture materials, further enhancing the carbon sequestration capabilities of the concrete. The inclusion of metakaolin also contributes to the overall sustainability of the mixture by reducing the need for energy-intensive cement production.\|[0079] Recycled Aggregates make up 20% of the composition, while Natural Aggregates constitute 15%. The use of recycled aggregates significantly reduces the environmental impact of the concrete production process by minimizing the need for new raw materials extraction. Natural aggregates provide the necessary mechanical strength to the concrete. The balance between recycled and natural aggregates is carefully optimized to maintain the structural integrity of the concrete while maximizing its sustainability.\|[0080] Silica Fume, at 2% of the mixture, fills micro-pores and enhances the strength and durability of the concrete. This component improves the overall pore structure of the concrete, which is crucial for both strength development and carbon sequestration potential. The fine particles of silica fume react with calcium hydroxide produced during cement hydration, forming additional calcium silicate hydrate (C—S—H) gel, which enhances the concrete's properties.\|[0081] Sodium Hydroxide (NaOH) and Sodium Silicate (Na2SiO3) serve as activators for the geopolymerization process, constituting 1.5% and 2.5% of the mixture respectively. These components are essential for activating the aluminosilicate materials in the mixture, particularly the fly ash and GGBFS. The careful balance of these activators ensures optimal reaction efficiency while minimizing environmental impact.\|[0082] Algae Biomass, used for creating alginate beads, makes up 2% of the mixture. This component is crucial for maximizing CO2 sequestration potential through the formation of alginate beads and direct air capture. The algae biomass is transformed into alginate beads through a process called ionic gelation, which dramatically increases the surface area available for CO2 absorption.\|[0083] Calcium Carbonate (CaCO3) and Magnesium Carbonate (MgCO3) each constitute 2% of the mixture. These components enhance carbonation during curing and beyond, improving overall CO2 capture. They react with CO2 to form stable carbonate compounds, effectively sequestering carbon within the concrete structure.\|[0084] Silica from Algae, comprising 1% of the mixture, serves as a sustainable silica source that improves strength with minimal environmental impact. This component contributes to the overall sustainability of the concrete mixture while enhancing its mechanical properties.\|[0085] Magnesium Silicate and Olivine (finely ground) each make up 1% of the mixture. These components enhance CO2 sequestration through mineral carbonation. The fine grinding of olivine increases its surface area, making it more reactive and efficient in capturing CO2. These materials react with atmospheric CO2 to form stable carbonate minerals, effectively locking away carbon for long periods.\|[0086] Basalt Rock Dust, constituting 1% of the mixture, provides trace minerals and enhances CO2 uptake through mineral carbonation. This component contributes to the overall carbon sequestration potential of the concrete while also improving its mechanical properties.\|[0087] Biochar (Activated) makes up 1% of the mixture. This component sequesters carbon and improves internal curing of the concrete. Biochar's porous structure allows it to absorb and retain CO2, contributing significantly to the overall carbon sequestration capabilities of the concrete.\|[0088] Alginate Beads, maximized at 1.5% of the mixture, play a crucial role in enhancing CO2 capture. These beads, formed through ionic gelation of brown algae powder, dramatically increase the surface area available for CO2 absorption. They form a matrix across the concrete surface, significantly enhancing long-term sequestration and improving durability.\|[0089] Carbonation Accelerators (C—S—H Seeds) constitute 1.5% of the mixture. These accelerate strength gain and CO2 uptake during curing. The C—S—H seeds provide nucleation sites for the formation of additional calcium silicate hydrate gel, which not only enhances the concrete's strength but also increases its capacity to absorb CO2.\|[0090] Water, making up 1% of the mixture, is necessary for workability and chemical reactions. The water content is carefully controlled to ensure optimal hydration of cementitious materials and proper workability of the concrete mix, while also facilitating the various chemical reactions involved in CO2 sequestration.\|[0091] This embodiment of the carbon-sequestering concrete composition demonstrates superior carbon sequestration capabilities compared to conventional concrete. For every 1,000 tons of concrete produced, this embodiment emits 81.4 tons of CO2 but sequesters 91.25 tons of CO2, resulting in a net sequestration of 9.85 tons of CO2. This represents a total reduction of 909.85 tons of CO2 per 1,000 tons produced, or a 101.1% reduction compared to conventional concrete.\|[0092] The CO2 sequestration in this embodiment occurs through several mechanisms, including biochar absorption, algae biomass uptake, carbonates reaction, mineral carbonation, alginate bead absorption, and CO2 absorption during curing. The total CO2 sequestered amounts to 91,250 kg (91.25 tonnes) per 1,000 tons of concrete produced.\|[0093] The carbon-sequestering concrete composition described in this embodiment demonstrates remarkable carbon sequestration capabilities that significantly outperform conventional concrete. For every 1,000 tons of concrete produced, this innovative composition achieves a net carbon sequestration of 9.85 tons of CO2, in stark contrast to conventional concrete which emits approximately 900 tons of CO2 for the same amount produced. This results in a total reduction of 909.85 tons of CO2 per 1,000 tons produced, representing a 101.1% reduction compared to conventional concrete.\|[0094] The superior carbon sequestration performance of this concrete composition is achieved through a combination of reduced emissions during production and active carbon capture mechanisms. While the embodiment emits 81.4 tons of CO2 during production, it sequesters 91.25 tons of CO2, resulting in the net negative carbon footprint. This remarkable feat is accomplished through several key mechanisms that work synergistically to capture and store carbon dioxide.\|[0095] The CO2 sequestration in this embodiment occurs through several primary mechanisms, including the following: Biochar absorption, which accounts for 29,333 kg of CO2 sequestered. The activated biochar in the mixture acts as a highly effective carbon sink due to its porous structure and high surface area. Algae Biomass uptake, responsible for sequestering 36,667 kg of CO2. The algae biomass, particularly when transformed into alginate beads, provides a substantial contribution to the overall carbon capture capacity of the concrete. Carbonates Reaction, which sequesters 2,000 kg of CO2. This involves the reaction of CO2 with calcium and magnesium carbonates present in the mixture, forming stable carbonate compounds. Mineral Carbonation, accounting for 2,500 kg of CO2 sequestered. This process involves the reaction of CO2 with minerals such as magnesium silicate and olivine to form stable carbonate minerals. Alginate Beads, which directly capture 750 kg of CO2 but also play a crucial role in enhancing the capture efficiency of other materials. The alginate beads, formed through ionic gelation of brown algae powder, create a matrix across the concrete surface that significantly increases the surface area available for CO2 absorption. CO2 absorbed during curing, which accounts for 20,000 kg of the total CO2 sequestered. This substantial amount is captured during the initial setting and hardening phase of the concrete.\|[0096] These mechanisms in an embodiment collectively result in a total CO2 sequestration of 91,250 kg (91.25 tonnes) per 1,000 tons of concrete produced. The synergistic interactions between the various components, particularly the alginate beads and other concrete constituents like geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS), enhance pozzolanic reactions and create additional sites for carbon dioxide capture. Furthermore, the moisture retention properties of the alginate beads create localized high-humidity environments within the concrete, facilitating greater direct air capture of CO2 throughout the concrete's service life.\|[0097] This innovative concrete composition not only addresses the carbon emissions associated with concrete production but also actively removes CO2 from the atmosphere, representing a significant advancement in sustainable construction materials.\|[0098] This embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0099] The alginate beads, formed through ionic gelation of brown algae powder, play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0100] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0101] By incorporating these innovative features, this embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0102] An alternative embodiment of the present invention comprises a carbon-sequestering concrete composition with the following components and their respective percentages by mass\| - Fly Ash (Class F): 22%\| - Ground Granulated Blast Furnace Slag (GGBFS): 20%\| - Metakaolin: 4%\| - Recycled Aggregates: 20%\| - Natural Aggregates: 12%\| - Silica Fume: 3%\| - Sodium Hydroxide (NaOH): 1%\| - Sodium Silicate (Na2SiO3): 2%\| - Algae Biomass (for Beads): 3%\| - Calcium Carbonate (CaCO3): 3%\| - Magnesium Carbonate (MgCO3): 3%\| - Silica from Algae: 1%\| - Magnesium Silicate: 2%\| - Olivine (Finely Ground): 3%\| - Basalt Rock Dust: 2%\| - Biochar (Activated): 2%\| - Alginate Beads (Maximized): 3%\| - Carbonation Accelerators (C—S—H Seeds): 2%\| - Water: 1%\|[0122] In this alternative embodiment, the Fly Ash (Class F) content is reduced to 22% in such embodiment to allow for increased CO2-reactive materials. This adjustment maintains the primary binding function while enhancing the overall carbon sequestration potential of the concrete. The Ground Granulated Blast Furnace Slag (GGBFS) in such embodiment is included at 20%, continuing to enhance strength and durability while acting as a supplementary binder. This component contributes significantly to reducing the carbon footprint associated with concrete production. Metakaolin is reduced to 4% in such embodiment, still improving early strength and reducing permeability while allowing for more CO2 capture materials. This adjustment contributes to the overall sustainability of the mixture. The ratio of Recycled Aggregates to Natural Aggregates is adjusted to 20% and 12% respectively in accordance with such embodiment. This change further reduces the environmental impact of the concrete production process while maintaining necessary mechanical strength. Silica Fume is increased to 3% to enhance the pore structure, strength, and durability of the concrete. This increase improves the overall performance and CO2 sequestration potential. The activators, Sodium Hydroxide (NaOH) and Sodium Silicate (Na2SiO3), are adjusted to 1% and 2% respectively. This optimization balances the geopolymerization process while minimizing environmental impact. Algae Biomass for beads is increased to 3%, maximizing CO2 sequestration potential through enhanced alginate bead formation and direct air capture. Both Calcium Carbonate (CaCO3) and Magnesium Carbonate (MgCO3) are increased to 3% each in accordance with this embodiment, enhancing carbonation during curing and beyond, thus improving overall CO2 capture. Magnesium Silicate is increased to 2%, and Olivine (Finely Ground) to 3%, enhancing CO2 sequestration through increased mineral carbonation potential. Basalt Rock Dust is increased to 2%, providing more trace minerals and enhancing CO2 uptake through mineral carbonation. Biochar (Activated) is increased to 2%, improving carbon sequestration and internal curing of the concrete. Alginate Beads are included at 3% in accordance with such embodiment, significantly enhancing CO2 capture and improving the concrete's overall performance. Carbonation Accelerators (C—S—H Seeds) are increased to 2%, further accelerating strength gain and CO2 uptake during curing. Water content remains at 1%, maintaining the necessary workability and facilitating chemical reactions.\|[0123] This alternative embodiment demonstrates enhanced carbon sequestration capabilities. For every 1,000 tons of concrete produced, this embodiment creates approximately 64.2 tons of CO2 but sequesters 101 tons of CO2 through direct air capture (DAC) and mineralization. This results in a net sequestration of approximately 36.8 tons of CO2 per 1,000 tons of concrete produced in accordance with an exemplary implementation.\|[0124] The carbon sequestration in this embodiment occurs through several mechanisms, including biochar absorption, algae biomass uptake, carbonates reaction, mineral carbonation, alginate bead absorption, and CO2 absorption during curing. The total CO2 sequestered amounts to 101,000 kg (101 tonnes) per 1,000 tons of concrete produced.\|[0125] This embodiment leverages the synergistic interactions between the alginate beads and other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag (GGBFS). These interactions enhance pozzolanic reactions, create additional sites for carbon dioxide capture, and prolong the period of CO2 absorption.\|[0126] The alginate beads, formed through ionic gelation of brown algae powder, play a crucial role in moisture retention, creating localized high-humidity environments within the concrete that facilitate greater direct air capture of CO2. This moisture retention is essential for the carbon sequestration process, as it provides a medium for CO2 to dissolve and react with calcium ions to form stable calcium carbonate.\|[0127] The formation of stable calcium carbonate through the interaction of dissolved CO2 with calcium ions contributes to the self-healing of micro-cracks in the concrete, further extending its lifespan and durability in an embodiment. This self-healing property maintains the concrete's ability to absorb CO2 over a longer period by preserving the integrity of the concrete structure.\|[0128] By incorporating these innovative features and optimizing the component ratios, this alternative embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|[0129] The carbon-sequestering concrete composition described in the embodiments of the invention in an example is designed to maximize eligibility for significant tax credits and incentives, potentially resulting in substantial cost savings for concrete producers and users. In an example, the tax credits could be allocated for 1,000 tons of concrete produced as an embodiment of the invention in accordance with the following:\|[0130] Section 45Q tax credits could provide approximately $100,000 to $150,000 in savings per 1,000 tons of concrete produced, depending on the final determination by the EPA/IRS and the results of a Life Cycle Assessment (LCA). This estimate is based on the net carbon sequestration capabilities of the concrete, which ranges from 9.85 to 36.8 tons of CO2 per 1,000 tons of concrete produced, depending on the specific embodiment.\|[0131] The Investment Tax Credit could cover up to 30% of a concrete mixer's investment in this carbon-sequestering concrete technology. This credit would apply to the capital expenditures required to implement the new production methods and equipment necessary for manufacturing this innovative concrete.\|[0132] Additional tax incentives that may be applicable in association with and as an expected benefit of an embodiment of the invention include:\|[0133] R&D tax credits for the ongoing development and improvement of the carbon-sequestering concrete technology. Production Tax Credits for the manufacture of environmentally beneficial products. Various federal and state tax incentives designed to promote sustainable construction practices and materials.\|[0134] When considering a larger scale of production, for example 20 medium sized building construction projects, the total savings from these combined tax credits and incentives could exceed $5 million for a concrete producer. This estimate takes into account the cumulative effect of the various tax benefits across multiple projects.\|[0135] The economic benefits of these tax credits extend beyond mere cost savings. They also enhance the competitiveness of the carbon-sequestering concrete in the market. Before applying any tax credits, the price of this innovative concrete is approximately $138 per ton, which is already competitive with conventional concrete. However, after factoring in the tax credits, the effective price drops to around $112 per ton, making it more economical than conventional concrete options.\|[0136] In accordance with various embodiments, the exact allocation and amount of tax credits may vary depending on factors such as the specific project details, the concrete producer's financial situation, and any changes in tax laws or regulations. Additionally, the realization of these tax benefits would likely require careful documentation of the carbon sequestration capabilities of the concrete, as well as compliance with relevant regulatory requirements, which is an intended use in accordance with an embodiment of the invention.\|[0137] Another embodiment of the invention comprises a carbon-sequestering concrete composition optimized for maximum CO2 sequestration and economic viability through tax incentives, as follows:\|[0138] The composition of this carbon-sequestering concrete in such embodiment is carefully formulated to maximize both CO2 sequestration capabilities and eligibility for tax credits. The mixture, designed for a 1,000-ton batch, comprises several key components that work synergistically to achieve these goals.\|[0139] Aluminosilicate materials form the foundation of the geopolymer binder system in such embodiment. These include 30% Fly Ash (Class F), 20% Ground Granulated Blast Furnace Slag (GGBFS), 5% Metakaolin, and 3% Silica Fume. These materials not only contribute to the strength and durability of the concrete but also play a crucial role in CO2 sequestration through pozzolanic reactions.\|[0140] A significant portion of the mix in such embodiment is dedicated to CO2-absorbing materials. This includes 15% Magnesium Silicate, 15% finely ground Olivine, 10% Activated Biochar, 3% Calcium Carbonate (CaCO3), and 2% Magnesium Carbonate (MgCO3). These components are specifically chosen for their high CO2 sequestration potential and their ability to form stable carbonate compounds over time.\|[0141] The aggregate portion of the mix consists of 10% Natural Aggregates and 5% Recycled Aggregates, balancing structural requirements with sustainability considerations in accordance with such embodiment. The alkaline activators, crucial for the geopolymerization process, include 2% Sodium Hydroxide (NaOH) and 4% Sodium Silicate (Na2SiO3).\|[0142] A key innovation in this embodiment is the incorporation of algae-derived components. This comprises 1% Silica from Algae, 3% Algae Biomass for bead formation, and 5% Alginate Beads. These components significantly enhance the CO2 sequestration capabilities of the concrete through increased surface area and the creation of localized high-humidity environments that facilitate CO2 absorption.\|[0143] The mixture in such embodiment also comprises 2% Carbonation Accelerators in the form of C—S—H Seeds, which enhance the rate of CO2 uptake during the curing process. The water content is maintained at 5%, with small amounts of superplasticizers (0.5%) and air-entraining agents (0.1%) added to optimize workability and durability.\|[0144] The production process of this concrete composition in such embodiment has been observed by the inventor to result in total emissions of 108,550 kg CO2 per 1,000 tons produced. However, the CO2 sequestration capabilities of the mixture are substantial, with a total CO2 sequestration potential of 435,000 kg CO2 per 1,000 tons of concrete. This results in a net negative carbon footprint of −326,450 kg CO2 per 1,000 tons of concrete produced in accordance with inventor observations.\|[0145] The CO2 sequestration occurs through several mechanisms in accordance with such embodiment. The Magnesium Silicate and Olivine each sequester 45,000 kg CO2. The Activated Biochar contributes significantly with 200,000 kg CO2 sequestered. The Algae Biomass and Alginate Beads together sequester 80,000 kg CO2. The Calcium and Magnesium Carbonates add another 5,000 kg CO2 to the total. Additionally, the CO2 curing process is estimated to sequester an additional 50,000 kg CO2.\|[0146] This embodiment is designed to maximize eligibility for tax credits, particularly the Section 45Q tax credit for carbon oxide sequestration. For every 1,000 tons of concrete produced, this composition is eligible for approximately $26,100 in Section 45Q tax credits. When combined with other available tax credits such as the Investment Tax Credit and R&D credits, the total tax credits per 1,000 tons could reach approximately $354,100 in accordance with the regulations in place as of September 2024.\|[0147] The economic viability of this concrete composition in such embodiment is further enhanced by these tax incentives. After accounting for all applicable tax credits, the effective cost of this concrete is estimated to be $57.85 per ton, making it highly competitive in the market.\|[0148] In comparison to other carbon-reducing concrete technologies, this embodiment demonstrates superior performance. For instance, when compared to Blue Planet's concrete, which sequesters 330 tons CO2 per 1,000 tons of concrete, this embodiment sequesters 435 tons CO2. This results in higher eligibility for Section 45Q tax credits and overall tax credits under applicable regulations in place in September 2024.\|[0149] The enhanced CO2 sequestration capabilities of this concrete composition in such embodiment are achieved through the synergistic interactions between its components, particularly the alginate beads and other concrete constituents like geopolymers, fly ash, and ground granulated blast furnace slag. These interactions enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The moisture retention properties of the alginate beads create localized high-humidity environments within the concrete, facilitating greater direct air capture of CO2 throughout the concrete's service life.\|[0150] This innovative concrete composition in accordance with such embodiment not only addresses the carbon emissions associated with concrete production but also actively removes CO2 from the atmosphere, representing a significant advancement in sustainable construction materials. Its superior carbon sequestration capabilities, combined with its economic viability through tax incentives, position it as a potentially disruptive technology in the concrete industry.\|[0151] The carbon-sequestering concrete composition described in the embodiment can be formulated with varying proportions of its key components to optimize performance and CO2 sequestration capabilities. The aluminosilicate materials, which form the foundation of the geopolymer binder system, can range from 30-60% of the total composition. This range allows for flexibility in adjusting the mix based on specific project requirements and material availability. The CO2-absorbing materials, crucial for the concrete's carbon sequestration properties, can constitute 30-50% of the mixture. This range ensures a significant portion of the concrete is dedicated to active CO2 absorption while maintaining structural integrity.\|[0152] The aggregate portion, balancing structural requirements with sustainability considerations, can range from 10-20% of the total composition in accordance with such embodiment. The alkaline activators, essential for the geopolymerization process, can comprise 5-10% of the mixture. The innovative algae-derived components, which significantly enhance CO2 sequestration capabilities, can make up 5-15% of the composition. This range allows for optimization of the algae-based materials' contribution to carbon capture. Carbonation accelerators can be included at 1-5% to enhance CO2 uptake during curing, while water content can be maintained between 4-6% to ensure proper workability and hydration.\|[0153] These ranges have been determined through extensive experimentation and observation by the inventor. They allow for the concrete composition in accordance with such embodiment to sequester at least 400 kg of CO2 per 1,000 kg of concrete produced, achieving a net negative carbon footprint of at least 300 kg CO2 per 1,000 kg of concrete. This flexibility in composition enables the concrete to be tailored for specific applications while maintaining its superior carbon sequestration capabilities and economic viability through tax incentives.\|[0154] The innovative features incorporated in the preferred embodiment address the limitations of previous approaches and provide a concrete composition with superior carbon sequestration capabilities. The use of brown algae-derived alginate beads, their synergistic interactions with other concrete components, and the enhanced moisture retention properties all contribute to a more effective and long-lasting carbon capture solution. This advanced concrete formulation not only reduces the carbon footprint associated with concrete production but also actively removes CO2 from the atmosphere throughout its service life, representing a significant step forward in sustainable construction materials.\|[0155] While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. It is not intended that the invention be limited by the specific examples provided within the specification. While the invention has been described with reference to the aforementioned specification, the descriptions and illustrations of the embodiments herein are not meant to be construed in a limiting sense. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. Furthermore, it shall be understood that all aspects of the invention are not limited to the specific depictions, configurations or relative proportions set forth herein which depend upon a variety of conditions and variables. It should be understood that various alternatives to the embodiments of the invention described herein may be employed in practicing the invention. It is therefore contemplated that the invention shall also cover any such alternatives, modifications, variations or equivalents. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby.	Family Number\|(112475776)\|112475776\|Abstract\|(US20250250199 A1)\|A carbon-sequestering concrete composition and method of production are disclosed. The composition comprises geopolymer binder components, aggregates, and alginate beads formed from brown algae powder through ionic gelation. The alginate beads significantly increase CO2 absorption surface area compared to algae powder, creating a matrix across the concrete surface that enhances long-term sequestration and improves durability. The beads interact synergistically with other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag, to enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The alginate beads also facilitate the dissolution of minerals like olivine, further enhancing carbon capture. The composition demonstrates superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. The method includes forming alginate beads, incorporating them into the concrete mixture, and allowing for initial hardening and drying processes that promote carbon dioxide absorption directly from the air.\|Advantages / Prev. Drawbacks\|(US20250250199 A1)\| (...) The use of brown algae provides a more efficient and targeted approach to carbon sequestration in concrete, leveraging their natural adaptations to marine environments.\|By addressing the limitations of previous approaches, this invention represents a significant advancement in sustainable construction materials, offering superior carbon sequestration capabilities, enhanced durability, and improved overall performance.\|By incorporating these innovative features, the preferred embodiment addresses the limitations of previous approaches and provides a concrete composition with superior long-term carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life.\|Independent Claims\|(US20250250199 A1)\| (...) at least one carbon dioxide sequestration enhancer selected from the group consisting of biochar, calcium carbonate, magnesium carbonate, magnesium silicate, olivine, and basalt rock dust.\|	Materials, metallurgy\|Other special machines	B28B-001/14\|B28B-001/54\|B28C-009/00/2\|C04B-012/00/5\|C04B-014/04/2\|C04B-014/06\|C04B-014/10/6\|C04B-014/26\|C04B-018/02/2\|C04B-018/08\|C04B-018/14/2\|C04B-022/00863\|C04B-022/10\|C04B-024/38\|C04B-028/00/6\|C04B-028/00/8\|C04B-040/00/32\|C04B-040/02/31\|C04B-2103/10\|C04B-2103/304\|C04B-2103/32\|C04B-2111/00017\|C04B-2111/00019\|C04B-2111/0075\|C04B-2111/1037\|C04B-2111/1093\|C04B-2111/29\|E01C-007/14/2\|Y02C-020/40\|Y02W-030/91	(GR1) C04B-028/00/6[RK1]; C04B-012/04[RK2]; C04B-014/04/2[RK3]; C04B-014/26[RK4]; C04B-014/28[RK5]; C04B-018/02/2[RK6]; C04B-018/08[RK7]; C04B-018/10/1[RK8]; C04B-018/14/1[RK9]; C04B-018/14/6[RK10]; C04B-022/06/4[RK11]; C04B-040/02/31[RK12]; C04B-2103/10[RK13]; C04B-2103/304[RK14]; C04B-2103/32[RK15]\|(GR1) C04B-028/00/6[RK1]; C04B-014/02[RK2]; C04B-014/06[RK3]; C04B-014/10/6[RK4]; C04B-018/08[RK5]; C04B-018/14/1[RK6]; C04B-018/14/6[RK7]; C04B-018/24/8[RK8]; C04B-020/00/8[RK9]; C04B-022/10[RK10]; C04B-040/00/28[RK11]\|(GR2) C04B-028/00/6[RK1]; C04B-012/04[RK2]; C04B-014/04/2[RK3]; C04B-014/26[RK4]; C04B-014/28[RK5]; C04B-018/08[RK6]; C04B-018/10/1[RK7]; C04B-018/14/1[RK8]; C04B-018/14/6[RK9]; C04B-022/06/4[RK10]; C04B-024/38[RK11]; C04B-040/02/31[RK12]; C04B-2103/10[RK13]; C04B-2103/304[RK14]; C04B-2103/32[RK15]\|(GR2) C04B-028/00/6[RK1]; C04B-014/02[RK2]; C04B-014/06[RK3]; C04B-014/10/6[RK4]; C04B-018/08[RK5]; C04B-018/14/1[RK6]; C04B-018/14/6[RK7]; C04B-018/24/8[RK8]; C04B-020/00/8[RK9]; C04B-040/00/28[RK10]	B28B-001/14\|B28B-001/54\|B28C-009/00/2\|C04B-012/00/5\|C04B-014/04/2\|C04B-014/06\|C04B-014/10/6\|C04B-014/26\|C04B-018/02/2\|C04B-018/08\|C04B-018/14/2\|C04B-022/00863\|C04B-022/10\|C04B-024/38\|C04B-028/00/6\|C04B-028/00/8\|C04B-040/00/32\|C04B-040/02/31\|C04B-2103/10\|C04B-2103/304\|C04B-2103/32\|C04B-2111/00017\|C04B-2111/00019\|C04B-2111/0075\|C04B-2111/1037\|C04B-2111/1093\|C04B-2111/29\|E01C-007/14/2\|Y02C-020/40\|Y02W-030/91	B28B-001/00\|C04B-012/00\|C04B-014/04\|C04B-014/06\|C04B-014/10\|C04B-014/26\|C04B-018/08\|C04B-018/14\|C04B-018/18\|C04B-022/00\|C04B-024/38\|C04B-026/00\|C04B-028/00\|C04B-040/00\|C04B-040/02\|C04B-103/10\|C04B-103/30\|C04B-103/32\|C04B-111/00	B28B-001/00\|C04B-012/00\|C04B-014/04\|C04B-014/06\|C04B-014/10\|C04B-014/26\|C04B-018/08\|C04B-018/14\|C04B-018/18\|C04B-022/00\|C04B-024/38\|C04B-026/00\|C04B-028/00\|C04B-040/00\|C04B-040/02\|C04B-103/10\|C04B-103/30\|C04B-103/32\|C04B-111/00			CN120365022\|CN120717739B	CN120365022 115400772 WHO=Examiner SELF=N CAT=A\|CN120717739B 116161526 WHO=Examiner SELF=N	KR102194390\|CN106465690\|KR102079643\|KR102043391	KR102194390 92039857 WHO=Examiner SELF=N CAT=Y CAT=A\|CN106465690 75568267 WHO=Examiner SELF=N CAT=Y CAT=A\|KR102079643 87699919 WHO=Examiner SELF=N CAT=X CAT=Y CAT=A\|KR102043391 86610040 WHO=Examiner SELF=N CAT=A		\|KR102079643; KR102194390; CN106465690; KR102043391		PENDING	(US20250250199)\|PENDING\|(WO2024/248905)\|PENDING	ALIVE	(US20250250199)\|ALIVE\|(WO2024/248905)\|ALIVE	(US20250250199)\|LEGAL DETAILS FOR US20250250199\|Actual or expected expiration date=2044-02-01\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-10-08\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US18909669\|Application date=2024-10-08\|Standardized application number=2024US-18909669\|Event publication date=2024-10-08\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2024-10-08\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2024-10-08\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 00004-Lafave_FTNPCIP\|Event publication date=2024-10-08\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 193636\|Event publication date=2024-10-08\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2024-10-08\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2024-10-08\|Event code=US/TR1RQ\|Event group=ACL Examination events\|TrackOne Accelerated Request\|Event publication date=2024-10-08\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2024-10-08\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2024-10-17\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2024-11-12\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2024-12-16\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2024-12-19\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2025-01-18\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-01-18\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-02-11\|Event code=US/TR1RQ\|Event group=ACL Examination events\|TrackOne Accelerated Request\|Event publication date=2025-03-08\|Event code=US/PDTD\|Event group=ACL Examination events\|Petition Decision Track 1 Deny\|Event publication date=2025-03-10\|Event code=US/PTDI\|Event group=OAO\|Petition Decision - Dismissed\|Event publication date=2025-08-07\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250250199\|Publication stage code=A1\|Publication date=2025-08-07\|Standardized publication number=US20250250199\|Event publication date=2025-08-07\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|(WO2024/248905)\|LEGAL DETAILS FOR WO2024/248905\|Actual or expected expiration date=2026-11-26\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-02-01\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2024/013913\|Application date=2024-02-01\|Standardized application number=2024WO-US13913\|Event publication date=2024-12-05\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2024/248905\|Publication stage code=A1\|Publication date=2024-12-05\|Standardized publication number=WO2024248905\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2025-12-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2025-12-30\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2044-02-01\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP24816062\|Event publication date=2025-01-15\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP	(WO2024/248905)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2024/248905)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2024/248905)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2024/248905)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2024/248905)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(US20250250199)\|US\|(WO2024/248905)\|WO; EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcNMYj8VpXFMrTkuDREcUBY0JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000022921030&ekey=2315&xpn=US20250250199&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/18909669/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=zeXk%252BPpISmS9OMQa8KBDm8RHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(US20250250199)\|US\|(WO2024/248905)\|US	(US20250250199)\|NAME=Lafave Michael , CITY=Denvor , STATE=CO , COUNTRY=US\|(WO2024/248905)\|NAME=LAFAVE, Michael 3000 E 112th Ave. Unit 2 Denver, Colorado 80233 , COUNTRY=US	(WO2024/248905)\|US	(WO2024/248905)\|NAME=SCHELL, Jeffrey 2128 W 32nd Ave., 2nd Floor Denver, Colorado 80211 , POSTCODE=80211 , COUNTRY=US	(US20250250199)\|US\|(WO2024/248905)\|US	(US20250250199)\|NAME=Lafave Michael, CITY=Denvor, STATE=CO , COUNTRY=US\|(WO2024/248905)\|NAME=LAFAVE, Michael 3000 E 112th Ave. Unit 2 Denver, Colorado 80233, POSTCODE=80233, COUNTRY=US	(US20250250199)\|2\|(WO2024/248905)\|2	4	2					(US20250250199)\|Number of Claims: NCL=20\|Number of Drawings: NDR=2\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1,6,11,15\|Number of Independent Claims: NICL=4\|Exemplary Claim Number: ECL=1\|\|(WO2024/248905)\|Number of Claims: NCL=38\|Extended kind: EXTK=x\|	(US20250250199)\|CIP of: US18/814,312 FDD=2024-08-23 [2024US-18814312]\|Continuation of: WOUS2024/013913 FDD=2024-02-01 [2024WO-US13913] PENDING	(US20250250199)\|ENGLISH (ENG)	(US20250250199)\|Patent\|(WO2024248905)\|Patent	Titre: (US20250250199)\|Carbon-Sequestering Concrete Composition with Enhanced CO2 Absorbtion and Method of Manufacturing Thereof Résumé: (US20250250199)\|A carbon-sequestering concrete composition and method of production are disclosed. The composition comprises geopolymer binder components, aggregates, and alginate beads formed from brown algae powder through ionic gelation. The alginate beads significantly increase CO2 absorption surface area compared to algae powder, creating a matrix across the concrete surface that enhances long-term sequestration and improves durability. The beads interact synergistically with other concrete components, including geopolymers, fly ash, and ground granulated blast furnace slag, to enhance pozzolanic reactions and create additional sites for carbon dioxide capture. The alginate beads also facilitate the dissolution of minerals like olivine, further enhancing carbon capture. The composition demonstrates superior carbon sequestration capabilities, enabling sustained CO2 absorption throughout its service life. The method includes forming alginate beads, incorporating them into the concrete mixture, and allowing for initial hardening and drying processes that promote carbon dioxide absorption directly from the air.	29	Abstract	gpt-4o-mini	no	The article focuses on a concrete composition for carbon sequestration, which falls under materials for construction rather than accelerated weathering of minerals for CO2 capture.
30	CN201611128528	CN201611128528	CN106757119\|CN106757119	76279049	CN106757119 B 2019-02-26 [CN106757119B]\|CN106757119 A 2017-05-31 [CN106757119]	2016-12-09	2016-12-09	2019-02-26\|2017-05-31	(CN106757119B)\|2019-02-26	(CN106757119)\|2036-12-09	(CN106757119)\|One kind is for realizing CO2The electro-chemical systems that capture is sealed up for safekeeping with mineralising	(CN106757119)\|The invention belongs to the technical field of carbon resource capturing and storing and relates to a system for achieving CO2 capturing and mineralization through an electrochemical method. The system is structurally composed of three parts of a hydrodynamic force module, a reaction module and a control and display module. By means of the electrochemical technology of a steady state, a transient state and combination of the steady state and the transient state, silicate is converted into carbonate, and CO2 capturing and mineralization are achieved. The CO2 capturing and mineralization system is mainly used for relieving the increasing greenhouse effect, liquid flow drained by the system is alkaline, and treatment of ocean acidification of local areas is achieved at the same time. The system can also be used for adjusting the concentration of CO2 gas in a closed space in real time and can also serve as an auxiliary facility for emission reduction of large CO2 emission enterprises.	DALIAN INSTITUTE OF CHEMICAL PHYSICS CHINESE ACADEMY OF SCIENCES\|DALIAN UNIVERSITY OF TECHNOLOGY	(CN106757119)\|DALIAN UNIVERSITY OF TECHNOLOGY ([CN])\|DALIAN INSTITUTE OF CHEMICAL PHYSICS CHINESE ACADEMY OF SCIENCES\|(CN106757119)\|DALIAN UNIVERSITY OF TECHNOLOGY ([CN])\|DALIAN INSTITUTE OF CHEMICAL PHYSICS CHINESE ACADEMY OF SCIENCES	MAO QING\|CUI JIANMING\|HUANG YANQIANG\|LIU JIANJUN\|JING WEIYUN\|SHI YUE	(CN106757119)\|MAO QING\|CUI JIANMING\|HUANG YANQIANG\|LIU JIANJUN\|JING WEIYUN\|SHI YUE\|(CN106757119)\|MAO QING\|CUI JIANMING\|HUANG YANQIANG\|LIU JIANJUN\|JING WEIYUN\|SHI YUE	(CN106757119)\|MEI HONGYU;PATENT AGENCY CENTER OF DLUT\|Reg. Nb: 21200	(CN106757119)\|However, the application area of geological sequestration is limited, which is not only closely related to the formation of geological rock, but also has high cost for later monitoring and maintenance, and is easy to cause geological disasters if leakage occurs.\|	(CN106757119)\|1. For realizing CO2The electrochemical system for capture and mineralization sealing is characterized in that:the system comprises a fluid power module, a reaction module and a control and display module, wherein the fluid power module is connected with the reaction module and provides CO for the reaction module2The feed gas and the supplementary electrolyte and the reactant of (1); the reaction module is CO2The capture and mineralization sealing provides a reaction site, which comprises an anode chamber, a cathode chamber and a diaphragm; the anode chamber has electrodes, electrolyte, silicate and/or silicate-containing materialMinerals, electrodes and electrolyte are arranged in the cathode chamber; the anode chamber is separated from the cathode chamber by a diaphragm; the control and display module is simultaneously connected with the reaction module and the fluid power module, provides running electric power for the fluid power module, and simultaneously realizes a steady state or transient state and steady state combined electrochemical reaction mode for the reaction module, so that silicate is converted into carbonate, and CO is realized2Capturing and mineralizing and sealing; the diaphragm in the reaction module is a cation exchange membrane.\|	(CN106757119)\|In order to overcome the defects in the prior art, the invention provides a method for realizing CO2An electrochemical system for capturing, mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed; the liquid flow discharged after the system is operated is alkaline, and the treatment of ocean acidification problems in a designated area can be realized to a certain extent.\|The system consists of a fluid power module, a reaction module and a control and display module.\|	(CN106757119)\|MINERALIZATION SEALING(100,16)\|SAFEKEEPING(100,4)\|REACTION MODULE(86,30)\|MINERALIZATION SEQUESTRATION(84,10)\|CO2THE MINERALIZATION(79,1)\|OCEAN ACIDIFICATION TREATMENT(75,1)\|GEOLOGICAL SEQUESTRATION(64,2)\|GEOLOGICAL ROCK FORMATION(61,1)\|GEOLOGICAL ROCK(60,1)\|CATHODE CHAMBER(57,8)\|ANODE COMPARTMENT(57,2)\|GEOLOGICAL DISASTER(57,2)\|ANODE CHAMBER(56,9)\|OCEAN ACIDIFICATION(53,3)\|ELECTROLYTE(52,9)\|SILICATE(49,16)\|MIXED GAS2THE(49,2)\|LATE MONITORING(45,1)\|DIAPHRAGM(44,7)\|CO2A CONCENTRATION SENSOR(44,3)\|REACTION MODULE2THE(44,2)\|CARBON RESOURCE CAPTURE(44,1)\|MATERIALMINERAL(44,1)\|SINE WAVE(42,4)\|NATURAL ORE(42,1)\|REGIONAL AREA OCEAN ACIDIFICATION(41,1)\|EQUILIBRIUM TRANSPORT(37,1)\|TRANSIENT(36,7)\|REAGENT(33,7)\|SUPPLEMENT ELECTROLYTE(33,3)\|SENSOR DEVICETHE RESPONSE(31,1)\|FLUID POWER MODULE(29,14)\|AUXILIARY EQUIPMENT(29,1)\|ENTERPRISE EMISSION REDUCTION(27,1)\|DEFECT(26,1)\|CO2CAPTURE(25,1)\|REACTIONWHEN(25,1)\|REACTION SITE(24,3)\|TRIANGULAR WAVE(24,3)\|CO2CO(24,2)\|ALKALINITY(23,1)\|OLIVINE(22,2)\|ELECTROCHEMICAL REACTION MODE(21,2)\|CATION EXCHANGE MEMBRANE(20,2)\|ENCLOSURE(20,1)\|FLUID DYNAMIC MODULE(20,1)\|REACTOR(19,5)\|STEADY STATE(18,18)\|AIR2THE ABSORPTION(18,5)\|ELECTRICAL POWER(18,5)\|VOLTAGE INFORMATION(18,3)\|LIQUID STREAM(18,1)\|SLEIPNER GEOLOGICAL SEQUESTRATION PROJECT(18,1)\|COMBINED ELECTROCHEMICAL REACTION MODE(17,2)\|MICROBIAL ELECTROCHEMICAL CO2A CAPTURE(17,1)\|OCEAN ACIDIFICATION CO2THE(16,1)\|REACTION MODULE OPERATION MODE(15,7)\|SQUARE WAVE(15,4)\|WORKING CURRENT DENSITY(15,4)\|GEOLOGICAL SEQUESTRATION APPLICATION AREA(15,1)\|CO2AN ELECTROLYTIC CAPTURE(13,1)\|ELECTROCHEMICAL PROCESS2THE CAPTURE(13,1)\|FLUID MOVEMENT(13,1)\|POROUS ELECTRODE STRUCTURE(12,2)\|CO2THE ELECTROCHEMICAL CAPTURE(12,1)\|ELECTROCHEMICAL CO2THE CAPTURE(12,1)\|GEOLOGICAL DISASTER RISK(12,1)\|LARGE SCALE CO2DISCHARGE(12,1)\|SILICATE MINERALS2A CAPTURE(12,1)\|DENSITY2THE ABSORPTION(11,2)\|CO2SUBSEQUENT ELECTRODIALYSIS(11,1)\|ELECTROCHEMICAL METHOD2COMPARED(11,1)\|SILICATE ROCK RESERVE(11,1)\|SILICATE INCORPORATION(10,2)\|ANODE CHAMBER2THE(10,1)\|INTO2THE TRAPPING(10,1)\|OCEAN SEQUESTRATION(10,1)\|POROUS TEFLON MEMBRANE(10,1)\|REALIZING CO2ELECTROCHEMICAL(10,1)\|LIQUID LEVEL SENSOR(9,3)\|TEMPERATURE SENSOR(9,3)\|SENSING DEVICE(8,12)\|PRESSURE SENSOR(8,3)\|FLAT ELECTRODE STRUCTURE(8,2)\|GREENHOUSE EFFECT(8,2)\|CO2HAS EMISSION(8,1)\|DENSITIES2THE ABSORPTION(8,1)\|MARKET MATURITY(8,1)\|RESIDENTIAL BUILDING(8,1)\|SEQUESTRATION SITE(8,1)\|SILICATE NONADDITION(8,1)\|WORKING MEDIUM2THE MINERALIZATION PRODUCT(8,1)\|DISPLAY DEVICE(7,6)\|CALCIUM SILICATE INTRODUCTION(7,2)\|ELECTROLYTE MOLTEN SALT(7,2)\|GEOLOGICAL STORAGE(7,2)\|PLATINUM SHEET(7,2)\|ABSORPTION ELECTROLYSIS(7,1)\|ANHYDROUS LIF(7,1)\|CCS CORE(7,1)\|DEMONSTRATION PROJECT(7,1)\|FLUE GAS2BY(7,1)\|MEMBRANE ELECTROLYSIS(7,1)\|MICROPOROUS MEMBRANE(7,1)\|NORTH SEA NORWEGIAN(7,1)\|POTASSIUM FELDSPAR(7,1)\|SEQUESTRATION2HIGH CONCENTRATION COMPRESSION(7,1)\|SILICATE SPECIES GRAPH(7,1)\|SIGNAL CHANGE FREQUENCY RANGE(6,3)\|ANODE INCORPORATIONTHE ACIDIFICATION DEGREE(6,1)\|ANODE PH(6,1)\|APPLICATION AREA(6,1)\|AQUEOUS CARBONATE CAPTURE(6,1)\|CATHODE COMPARTMENT(6,1)\|CO2AFTER CALCIUM SILICATE(6,1)\|CO2CHEMICAL REACTION(6,1)\|ELECTRODIALYSIS2BY AQUEOUS SOLUTION(6,1)\|FIREPROOF COATING(6,1)\|FOSSIL FUEL COMBUSTION(6,1)\|GEOLOGICAL SEALING(6,1)\|INORGANIC ASH(6,1)\|INTERNATIONAL SOCIETY CONCERN(6,1)\|LI2CO3THE MOLAR RATIO(6,1)\|LIQUID FLOW(6,1)\|METHANEDIONE ELECTROCHEMICAL REDUCTION(6,1)\|OCEAN SEALING(6,1)\|ORGANIC WASTEWATER(6,1)\|POSITIVE PRESSURE2SOLVENT(6,1)\|PURITY CO2(6,1)\|REGENERATED CAPTURE SOLUTION(6,1)\|RELEASING TOWER(6,1)\|SEWAGE TREATMENT CO2THE(6,1)\|BICARBONATE(5,2)\|OCEAN STORAGE(5,2)\|TRANSPORTATION(5,2)\|ANION EXCHANGE MEMBRANE(5,1)\|CO2THE SEQUESTRATION(5,1)\|CO2THE SOLUTION(5,1)\|CONDITION2THE(5,1)\|DIOSMECTITE(5,1)\|DISCLOSED2THERE(5,1)\|FOAM COPPER(5,1)\|FOAM NICKEL(5,1)\|GAS REALTIME ADJUSTING(5,1)\|INTERMITTENT DISCHARGE MODE(5,1)\|MICROBIAL NUTRIENT SOURCE(5,1)\|MINERALIZATION PRODUCTION(5,1)\|NATURALLY OCCURRING SILICATE(5,1)\|NI ALLOY(5,1)\|NONMETAL(5,1)\|SYSTEM2THE AIR(5,1)\|SYSTEMTHE ANGULAR WAVE SIGNAL(5,1)\|MAGNESIUM SILICATE(4,3)\|STEADY STATE OPERATION MODE(4,3)\|TRANSIENT STATE OPERATION MODE(4,3)\|COMBINED OPERATION MODE(3,4)\|ABSORPTION STEADY STATE BEHAVIOR(3,1)\|AGALMATOLITE(3,1)\|ALKALINE EARTH OXIDE(3,1)\|ALUMINATE(3,1)\|ANOLYTE(3,1)\|ASBESTOS(3,1)\|BASALT(3,1)\|\|(CN106757119)\|MINERALIZATION SEALING(100,18)\|SAFEKEEPING(100,4)\|REACTION MODULE(76,31)\|CO2THE MINERALIZATION(70,1)\|OCEAN ACIDIFICATION TREATMENT(67,1)\|MINERALIZATION SEQUESTRATION(61,9)\|ELECTROCHEMICAL METHOD2THE(57,1)\|GEOLOGICAL SEQUESTRATION(56,2)\|GEOLOGICAL ROCK FORMATION(54,1)\|GEOLOGICAL ROCK(53,1)\|CATHODE CHAMBER(51,8)\|GEOLOGICAL DISASTER(51,2)\|ANODE CHAMBER(50,9)\|ANODE COMPARTMENT(50,2)\|ELECTROLYTE(47,9)\|OCEAN ACIDIFICATION(47,3)\|SILICATE(43,16)\|INVENTION2CAPTURE SEAL(41,1)\|CO2THE AUXILIARY EQUIPMENT(40,1)\|LATE MONITORING(40,1)\|CO2A CONCENTRATION SENSOR(39,3)\|REACTION MODULE2THE(39,2)\|MATERIALMINERAL(39,1)\|NATURAL ORE(38,1)\|SINE WAVE(37,4)\|REGIONAL AREA OCEAN ACIDIFICATION(36,1)\|DIAPHRAGM(34,7)\|TRANSIENT(33,7)\|SENSING DEVICEREACTION RESPONSE(31,1)\|MICROPOROUS MEMBRANE(30,2)\|SUPPLEMENT ELECTROLYTE(29,3)\|FLUID POWER MODULE(28,14)\|DISCHARGE ENTERPRISE EMISSION REDUCTION(26,1)\|REAGENT(25,6)\|ALKALESCENCE(23,1)\|DEFECT(23,1)\|CARBON RESOURCE(22,2)\|REACTION SITE(21,3)\|NONMETAL(20,2)\|ELECTRICAL POWER(19,6)\|TRIANGULAR WAVE(19,4)\|OLIVINE(19,2)\|EQUILIBRIUM(19,1)\|ELECTROCHEMICAL REACTION MODE(18,2)\|REACTOR(17,5)\|FLUID DYNAMIC MODULE(17,1)\|STABLEIN(17,1)\|AIR2THE ABSORPTION(16,5)\|MIXED GAS(16,3)\|VOLTAGE INFORMATION(16,3)\|SLEIPNER GEOLOGICAL SEQUESTRATION PROJECT(16,1)\|SYSTEM RELIEF LIQUOR STREAM(16,1)\|STEADY STATE(15,17)\|REACTION MODULE OPERATION MODE(15,8)\|COMBINED ELECTROCHEMICAL REACTION MODE(15,2)\|CLOSING SPACE(15,1)\|MICROBIAL ELECTROCHEMICAL CO2A CAPTURE(15,1)\|DISPLAY MODULE THREE(14,1)\|OCEAN ACIDIFICATION CO2THE(14,1)\|SQUARE WAVE(13,4)\|WORKING CURRENT DENSITY(13,4)\|GEOLOGICAL SEQUESTRATION APPLICATION AREA(13,1)\|CO2AN ELECTROLYTIC CAPTURE(12,1)\|COUNTER POWER(12,1)\|ELECTROCHEMICAL PROCESS2THE CAPTURE(12,1)\|CATION EXCHANGE MEMBRANE(11,2)\|POROUS ELECTRODE STRUCTURE(11,2)\|CO2THE ELECTROCHEMICAL CAPTURE(11,1)\|ELECTROCHEMICAL CO2THE CAPTURE(11,1)\|GEOLOGICAL DISASTER RISK(11,1)\|SILICATE MINERALS2A CAPTURE(11,1)\|DENSITY2THE ABSORPTION(10,2)\|CO2SUBSEQUENT ELECTRODIALYSIS(10,1)\|ELECTROCHEMICAL METHOD2COMPARED(10,1)\|LIQUID LEVEL SENSOR(8,3)\|TEMPERATURE SENSOR(8,3)\|ANODE CHAMBER2THE(8,1)\|INTO2THE TRAPPING(8,1)\|OCEAN SEQUESTRATION(8,1)\|POROUS TEFLON MEMBRANE(8,1)\|REALIZING CO2ELECTROCHEMICAL(8,1)\|PRESSURE SENSOR(7,3)\|FLAT ELECTRODE STRUCTURE(7,2)\|GREENHOUSE EFFECT(7,2)\|ACID ROCK CRUSTTHE RESERVE(7,1)\|CO2HAS EMISSION(7,1)\|DENSITIES2THE ABSORPTION(7,1)\|MARKET MATURITY(7,1)\|SEQUESTRATION SITE(7,1)\|SILICATE NONADDITION(7,1)\|WORKING MEDIUM2THE MINERALIZATION PRODUCT(7,1)\|DISPLAY DEVICE(6,6)\|CALCIUM SILICATE INTRODUCTION(6,2)\|ELECTROLYTE MOLTEN SALT(6,2)\|GEOLOGICAL STORAGE(6,2)\|PLATINUM SHEET(6,2)\|ABSORPTION ELECTROLYSIS(6,1)\|ANHYDROUS LIF(6,1)\|CCS CORE(6,1)\|DEMONSTRATION PROJECT(6,1)\|FLUE GAS2BY(6,1)\|MEMBRANE ELECTROLYSIS(6,1)\|NORTH SEA NORWEGIAN(6,1)\|POTASSIUM FELDSPAR(6,1)\|SEQUESTRATION2HIGH CONCENTRATION COMPRESSION(6,1)\|SILICATE SPECIES GRAPH(6,1)\|SIGNAL CHANGE FREQUENCY RANGE(5,3)\|ANODE PH(5,1)\|APPLICATION AREA(5,1)\|AQUEOUS CARBONATE CAPTURE(5,1)\|CATHODE COMPARTMENT(5,1)\|CO2AFTER CALCIUM SILICATE(5,1)\|CO2CHEMICAL REACTION(5,1)\|ELECTRODIALYSIS2BY AQUEOUS SOLUTION(5,1)\|FIREPROOF COATING(5,1)\|GAS REALTIME REGULATION(5,1)\|GEOLOGICAL SEALING(5,1)\|INORGANIC ASH(5,1)\|INTERNATIONAL SOCIETY CONCERN(5,1)\|LI2CO3THE MOLAR RATIO(5,1)\|LIQUID FLOW(5,1)\|METHANEDIONE ELECTROCHEMICAL REDUCTION(5,1)\|OCEAN SEALING(5,1)\|ORGANIC WASTEWATER(5,1)\|POSITIVE PRESSURE2SOLVENT(5,1)\|PURITY CO2(5,1)\|REGENERATED CAPTURE SOLUTION(5,1)\|RELEASING TOWER(5,1)\|SEWAGE TREATMENT CO2THE(5,1)\|BICARBONATE(4,2)\|OCEAN STORAGE(4,2)\|TRANSPORTATION(4,2)\|ANION EXCHANGE MEMBRANE(4,1)\|CALCIUM SILICATE INCORPORATION(4,1)\|CO2THE SEQUESTRATION(4,1)\|CO2THE SOLUTION(4,1)\|CONDITION2THE(4,1)\|DIOSMECTITE(4,1)\|DISCLOSED2THERE(4,1)\|FLOWTHE(4,1)\|FOAM COPPER(4,1)\|FOAM NICKEL(4,1)\|INTERMITTENT DISCHARGE MODE(4,1)\|MICROBIAL NUTRIENT SOURCE(4,1)\|MINERALIZATION PRODUCTION(4,1)\|NATURALLY OCCURRING SILICATE(4,1)\|NI ALLOY(4,1)\|SYSTEM2THE AIR(4,1)\|COMBINED OPERATION MODE(3,4)\|MAGNESIUM SILICATE(3,3)\|STEADY STATE OPERATION MODE(3,3)\|TRANSIENT STATE OPERATION MODE(3,3)\|ABSORPTION STEADY STATE BEHAVIOR(3,1)\|AGALMATOLITE(3,1)\|ALKALINE EARTH OXIDE(3,1)\|ALUMINATE(3,1)\|	(CN106757119)\|1. For realizing CO2The electrochemical system for capture and mineralization sealing is characterized in that:\|the system comprises a fluid power module, a reaction module and a control and display module, wherein the fluid power module is connected with the reaction module and provides CO for the reaction module2The feed gas and the supplementary electrolyte and the reactant of (1); the reaction module is CO2The capture and mineralization sealing provides a reaction site, which comprises an anode chamber, a cathode chamber and a diaphragm; the anode chamber has electrodes, electrolyte, silicate and/or silicate-containing materialMinerals, electrodes and electrolyte are arranged in the cathode chamber; the anode chamber is separated from the cathode chamber by a diaphragm; the control and display module is simultaneously connected with the reaction module and the fluid power module, provides running electric power for the fluid power module, and simultaneously realizes a steady state or transient state and steady state combined electrochemical reaction mode for the reaction module, so that silicate is converted into carbonate, and CO is realized2Capturing and mineralizing and sealing; the diaphragm in the reaction module is a cation exchange membrane.\|2. A method for the realization of CO according to claim 12The electrochemical system for trapping and mineralizing and sealing is characterized in that the electrode material comprises a simple substance, an alloy or a compound formed by other non-metallic elements, wherein the simple substance or the alloy contains Pt, Re, Pd, Rh, Mo, W, Nb, Ru, Ir, Sn, Mn, Fe, Co, Ni, Cu, Ag and C.\|3. A method for the realization of CO according to claim 1 or 22The electrochemical system for capture and mineralization sealing is characterized in that the anode is of a flat electrode structure or a porous electrode structure.\|4. A method for the realization of CO according to claim 1 or 22Electrochemical system for capture and mineralization sequestration characterized in that said anodic compartment is treated with CO2CO in mixed gas2The concentration range of (A) is between 0.050% and 99.995%.\|5. A method for the realization of CO according to claim 32Electrochemical system for capture and mineralization sequestration characterized in that said anodic compartment is treated with CO2CO in mixed gas2The concentration range of (A) is between 0.050% and 99.995%.\|6. A method for the realization of CO according to claim 1 or 2 or 52Electrochemical system for capture and mineralization sequestration, characterised by the reactionWhen the module operation mode is a steady state, the working current density range is 0.075mA/cm2～2A/cm2To (c) to (d); when the operation mode of the reaction module is transient, sine wave, square wave and triangular wave signals of current or voltage are loaded to the system, and the change frequency range of the signals is 1000 Hz-0.1 Hz.\|7. A method for the realization of CO according to claim 32The electrochemical system for capture and mineralization sealing is characterized in that when the operation mode of the reaction module is steady state, the working current density range is 0.075mA/cm2～2A/cm2To (c) to (d); when the operation mode of the reaction module is transient, sine wave, square wave and triangular wave signals of current or voltage are loaded to the system, and the change frequency range of the signals is 1000 Hz-0.1 Hz.\|8. A method for the realization of CO according to claim 42The electrochemical system for capture and mineralization sealing is characterized in that when the operation mode of the reaction module is steady state, the working current density range is 0.075mA/cm2～2A/cm2To (c) to (d); when the operation mode of the reaction module is transient, sine wave, square wave and triangular wave signals of current or voltage are loaded to the system, and the change frequency range of the signals is 1000 Hz-0.1 Hz.\|9. A process for the realization of CO according to claim 1 or 2 or 5 or 7 or 82The electrochemical system for capture and mineralization sealing is characterized in that the control and display module comprises a sensing device, a system control device and a display device; wherein the sensing device comprises H2、O2、CO2A concentration sensor, a temperature sensor, a liquid level sensor and a pressure sensor; the display device is used for displaying temperature, pressure and O in system operation2Concentration, H2Concentration, CO2Concentration, liquid level, current, voltage information; the system control device supplies electric power to the sensor device and controls fluid movement according to the response of the sensor deviceThe force module provides reactants and supplementary electrolyte for the reactor; on the other hand, a digital signal processor in the system control device controls the operation of the reactor, and provides a steady-state operation mode, a transient-state operation mode or a steady-state and transient-state combined operation mode for the system.\|10. A method for the realization of CO according to claim 32The electrochemical system for capture and mineralization sealing is characterized in that the control and display module comprises a sensing device, a system control device and a display device; wherein the sensing device comprises H2、O2、CO2A concentration sensor, a temperature sensor, a liquid level sensor and a pressure sensor; the display device is used for displaying temperature, pressure and O in system operation2Concentration, H2Concentration, CO2Concentration, liquid level, current, voltage information; on one hand, the system control device provides electric power for the sensing device and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a digital signal processor in the system control device controls the operation of the reactor, and provides a steady-state operation mode, a transient-state operation mode or a steady-state and transient-state combined operation mode for the system.	(CN106757119)\|TECHNICAL FIELD\|[0002] The invention belongs to the technical field of capture and storage of carbon resources, and relates to a method for realizing CO2Electrochemical system for capture and mineralization sequestration\|BACKGROUND ART\|[0004] CO excessively discharged in China2Mainly from fossil fuel combustion, e.g. for power generation, but also from small dispersed sources, e.g. automobile engines, and combustion in residential and commercial buildingsA furnace; in addition to this, CO2Also in the refining of certain mineral resources. Currently, excessive emission of CO2Has led to an increasingly severe greenhouse effect, due to the large part of CO2Gas is absorbed by the ocean, which makes the ocean acidification problem increasingly serious. The concern of the international society on climate change leads to the emergence of the framework convention of climate change of the united nations, and further promotes CO2Development of capture and sequestration technology (CCS) technology.\|[0005] CCS technology generally includes three major components of capture, transport and containment. First, the capture step is to capture CO2Separated from other gaseous products. Such as combustion processes in power plants, separation techniques may be employed to capture CO after combustion2Or decarbonizing the fuel prior to combustion. Secondly, in order to capture CO2Transport to CO2The source is far away from the appropriate sequestration site, requiring transportation steps to be taken. Captured CO for ease of transportation and sequestration2High concentration compression is typically performed by the capture device. Last CO2The sequestration process is the core of CCS technology, determining the overall process cost and process complexity. Currently, CO2The sealing technology comprises three types of geological sealing, ocean sealing and mineralization sealing, and the technology is greatly different from the maturity of the market. Geological sequestration technology is relatively mature, and currently, industrial demonstration projects are available, such as: the Norwegian North sea Sleipner geological sequestration project has successfully injected 1000 million tons of CO into the ground2. However, the application area of geological sequestration is limited, which is not only closely related to the formation of geological rock, but also has high cost for later monitoring and maintenance, and is easy to cause geological disasters if leakage occurs.\|[0006] Ocean sequestration and mineralization sequestration are currently only in the research, development, or demonstration stages. Among these, the mineralization sequestration technology has great potential to develop, which mainly utilizes the basic or alkaline earth oxides, such as magnesium oxide and calcium oxide, present in naturally occurring silicate rocks to sequester CO2And (5) curing. These substances are mixed with CO2Chemical reactions produce compounds such as magnesium carbonate and calcium carbonate. The advantages of mineralization and sequestration are as follows: (1) wide raw material sourceAnd 4. preparing the compound. On the one hand, the reserves of silicate rock in the crust are enormous, while these oxides may also be present in certain industrial wastes, such as stainless steel slag and mineral ash; (2) CO 22After mineralization, the mineral is not released into the atmosphere, compared with geological storage and ocean storage, the mineral is free from subsequent monitoring and maintenance cost, and the storage risk is small; (3) the mineralized carbonate product has wide application, can be used as building materials and fireproof coatings, is also an important chemical raw material, and is widely applied to the industries of chemical industry, glass, paper making and the like.\|[0007] CO presently disclosed2There are two main types of capture and mineralization sequestration techniques. One is achieved by chemical methods, while the other is based on electrochemical methods. The former is mostly carried out at high temperature or high pressure, and the system structure is complex. For example, Olsen Espen discloses the use of metal oxide salt solutions to absorb CO at temperatures between 600 ℃ and 1600 ℃2The technology and process of (CN 102448581A, US 20120128559). Terasaka et al (chem. Eng. Technol.2006, 29No 9, pp. 1118-4) Absorption of CO as a working medium2The mineralization product is Li2CO3And Li2SiO3In the form of suspended solid particles. US2005036932 discloses an absorption and removal of CO from flue gas2By bubbling the exhaust gas through a stream containing CaO and/or Ca (OH)2Of solid particles of (a) so that CO in the exhaust gas is present2Conversion to CaCO3. CN 102491795A discloses CO at 150-350 deg.C2Under the condition that the partial pressure is not lower than 1.0MPa, the potassium feldspar is used for leading CO to be treated2A method for producing a potassium-rich solution by mineralization; CN 102895847A discloses that CO is introduced into2The trapping method comprises introducing molten alkali metal, alkaline earth metal, transition metal carbonate, silicate, borate, oxide, hydroxide, nitrate, aluminate and their mixture into the reactor for absorption electrolysis. CN 103111161A discloses a larger scale CO2Capture process by CO with positive pressure2Solvent capture of CO in a capture column2Supersaturated CO2The solution enters a releasing tower again for extraction and concentration.CO based electrochemical process2The capture and conversion process is relatively simple and the operating environment is relatively mild, CN 101670236A discloses recovery of CO by aqueous carbonate capture and electrodialysis2By aqueous solution capture of CO2Subsequent electrodialysis to form CO-rich2Liquid flow and regenerated capture solution. CN 102351310A discloses microbial electrochemical CO2A capture system using organic wastewater as a microbial nutrient source in CO2The problem of sewage treatment is considered while the sewage is captured. CN 102978653A discloses a mineralized CO2The membrane electrolysis method for coproducing strong acid is characterized by that its mineralized raw material is nitrate or sulfate, and its product is carbonate and nitric acid. CN 105420751 a discloses a method for preparing hydrocarbons by electrochemical reduction of carbon dioxide, which uses alkali metal carbonate (bicarbonate), sulfate, phosphate (bicarbonate), etc. as substances and electrolyte, and is characterized in that an organic solvent is introduced into an electrolyte system. Unlike electrochemical capture in aqueous systems, CN 103590064 a discloses the use of anhydrous LiF and Li2CO3The molar ratio (0.5-1.5): 1, uniformly mixing, adding an additive to prepare electrolyte molten salt, placing the electrolyte molten salt in an electrolytic cell, heating to 690-700 ℃, and introducing CO2An electrolytic capture method. Wherein the cathode material is Ni or Ti, and the anode material is Pt, Fe-Ni alloy or Fe-Ni-Al2O3And (3) alloying.\|DISCLOSURE\|[0008] Disclosure of Invention\|[0009] In order to overcome the defects in the prior art, the invention provides a method for realizing CO2An electrochemical system for capturing, mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed; the liquid flow discharged after the system is operated is alkaline, and the treatment of ocean acidification problems in a designated area can be realized to a certain extent.\|[0010] Can realize CO2The technical scheme of the electrochemical system for capturing, mineralizing and sealing up comprises the following steps:\|[0011] the system comprises a fluid power module, a reaction module and a control and display module, wherein the fluid power module is connected with the reaction module and provides CO for the reaction module2The feed gas and the supplementary electrolyte and the reactant of (1); the reaction module is CO2The capture and mineralization sealing provides a reaction site, which comprises an anode chamber, a cathode chamber and a diaphragm; the anode chamber is internally provided with an electrode, electrolyte, silicate and/or mineral containing silicate, and the cathode chamber is internally provided with an electrode and electrolyte; the anode chamber is separated from the cathode chamber by a diaphragm; the control and display module is simultaneously connected with the reaction module and the fluid power module, provides running electric power for the fluid power module, and simultaneously realizes a steady state or transient state and steady state combined electrochemical reaction mode for the reaction module, so that silicate is converted into carbonate, and CO is realized2Capture and mineralize and seal up.\|[0012] The diaphragm in the reaction module comprises an anion-exchange membrane, a cation-exchange membrane or a microporous membrane (such as a porous polytetrafluoroethylene membrane); the electrode material comprises simple substances, alloys or compounds formed by other nonmetal elements containing Pt, Re, Pd, Rh, Mo, Wo, Nb, Ru, Ir, Sn, Mn, Fe, Co, Ni, Cu, Ag and C. The silicate includes all compounds or mixtures containing silicon, oxygen and other chemical elements (such as aluminum, iron, calcium, magnesium, manganese, potassium, sodium, barium, copper, zinc, lead, tin). The silicate-containing mineral includes olivine, serpentine, basalt, asbestos, mica, talc, kaolinite, montmorillonite, zeolite, agalmatolite, tourmaline, pyroxene, and hornblende containing the above silicate components.\|[0013] The anode is of a flat electrode structure or a porous electrode structure.\|[0014] CO treated in the anode chamber2The concentration range of the mixed gas is between 0.050% and 99.995%.\|[0015] When the operation mode of the reaction module is steady state, the working current density range is 0.075mA/cm2～2 A/cm2To (c) to (d); when the operation mode of the reaction module is transient, a sine wave, a square wave and a three wave of current or voltage are loaded on the systemThe angular wave signal has a variation frequency range of 1000 Hz-0.1 Hz.\|[0016] The control and display module comprises a sensing device, a system control device and a display device; wherein the sensing device comprises H2、O2、CO2A concentration sensor, a temperature sensor, a liquid level sensor and a pressure sensor; the display device is used for displaying temperature, pressure and O in system operation2Concentration, H2Concentration, CO2Concentration, level, current, voltage information; on one hand, the system control device provides electric power for the sensing device and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a digital signal processor in the system control device controls the operation of the reactor, and provides a steady-state operation mode, a transient-state operation mode or a steady-state and transient-state combined operation mode for the system.\|[0017] CO of system treatment2The concentration range of the gas is wide, namely high-concentration CO can be realized2(99.99%) conversion can also be used for trace amounts of CO in air2(ppm level) conversion, System CO2The transformation scale of (2) is controllable and modularization is easy to realize. The discharged product of the system after operation is environment-friendly and alkaline, and the system can realize CO2The problem of ocean acidification which is becoming more serious at present can be simultaneously relieved while the capture and the mineralization are sealed.\|[0018] The invention realizes CO by adopting an electrochemical method2Compared with the application of physical methods (including geological storage and ocean storage), the technology does not need to be monitored in the later period and has no risk of geological disasters. Compared with the existing applied chemical method to realize CO2Compared with the technology of capture and mineralization sealing, the invention applies the electrochemical method without high temperature and high pressure reaction environment, the reaction can be carried out at normal temperature and normal pressure, the system has simple structure and low energy consumption, and is easy to realize modular design and has huge application prospect.\|DRAWINGS DESCRIPTION\|[0020] FIG. 1 is CO2The structure of the electrochemical capture and mineralization sealing system is shown schematically.\|[0021] FIG. 2 is introduction of calcium silicate to CO in air2The absorption efficiency and the system cell pressure.\|[0022] FIG. 3 is a graph of silicate species vs. CO in the air of the system2The effect of the absorption effect of (c).\|[0023] FIG. 4 is a graph of the system versus CO in air at different current densities2The absorption effect of (1).\|[0024] Wherein (a) is CO2A time-dependent profile; (b) after 3 hours, CO2Concentration profile with system power.\|[0025] FIG. 5 shows 4mA cm of electrode material at room temperature for a system-2For CO in air under the condition2The effect of absorption.\|[0026] Wherein (a) is CO2The change in concentration over time; (b) is the change of the system tank pressure with time.\|[0027] FIG. 6 shows the system operating under unsteady state current conditions for CO in air2The absorption effect of (1).\|[0028] Wherein (a) is the variation of the system current with time; (b) is CO2The change in concentration with time.\|[0029] FIG. 7 is a graph of the system versus CO in air at low current density2The absorption effect of (1).\|[0030] FIG. 8 is a graph of system for high purity CO at high current density2The absorption effect of (1).\|INVENTION MODE\|[0031] Detailed Description\|[0032] To further illustrate the invention, the following examples are presented to describe CO2The electrochemical capture and containment system is not intended to limit the scope of the invention.\|INVENTION MODE\|[0033] Example 1: CO 22Electrochemical capture and containment system architecture\|[0034] FIG. 1 shows CO2And (3) an electrochemical capture and mineralization sequestration system structure. The system consists of a fluid power module, a reaction module and a control and display module. The fluid power module is connected with the reaction module and can be provided with CO2May also be supplemented with supporting electrolytes and reactants. The control and display module is simultaneously connected with the reaction module and the fluid power module, and the system controller provides electric power for the sensing device on one hand and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a Digital Signal Processor (DSP) in the controller can control the operation of the reactor, provide steady-state, transient-state, steady-state and transient-state combined operation modes for the system and realize shutdown operation. The reaction module is the core component of the system and is CO2The capture and mineralization sealing provides a reaction site, and the structure of the device consists of an anode chamber, a cathode chamber and a diaphragm. The anode chamber and the cathode chamber are respectively provided with an anode, an anolyte, a cathode and a catholyte, wherein the anode chamber contains silicate.\|INVENTION MODE\|[0035] Example 2: CO 22The electrochemical capture and mineralization sequestration system is the same as example 1, which compares the addition or non-addition of silicate to the system CO2Absorption efficiency and emission of products.\|[0036] FIG. 2 shows electrochemical CO with and without silicate minerals2A capture and mineralization sealing system with a current density of 2mA cm-2Under the condition, the system can be used for treating CO in the air2The absorption effect and the system tank pressure. It can be seen that the introduction of calcium silicate is for CO2The absorption and system power consumption effects of (1) produced significant results after 100 minutes, calcium silicate containing system exhaust gas CO2The concentration is relatively low. Table 1 shows the effect of silicate incorporation on the pH of the effluent after 8 hours of operation of the system, which is seen in calcium silicate incorporationThe acidification degree of the anode discharge product is obviously reduced.\|[0037] TABLE 1 Effect of silicate incorporation on the pH of the anode and cathode compartments\|[0038] \|INVENTION MODE\|[0039] Example 3: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, in this example, silicate species are compared to system CO2The absorption efficiency of (a).\|[0040] FIG. 3 shows the reaction at CO2After calcium silicate, magnesium silicate, aluminum silicate and sodium silicate are introduced into the electrochemical capture and mineralization sealing system, the system can be used for treating CO in the air at room temperature2Comparison of absorption effects. The reaction module is operated in a steady-state constant current mode in the system operation, and the current is 2 mA-cm-2. It can be seen that the type of silicate affects the system CO2Transient and steady state behavior of the absorption. System Pair CO introducing aluminum silicate and magnesium silicate 1 hour after system startup2The absorption effect is inferior to that of the system containing calcium silicate and sodium silicate. After 3 hours of operation, the system had entered steady state, with systems employing magnesium silicate for CO2The absorption effect of (A) is inferior to that of the other three silicates.\|INVENTION MODE\|[0041] Example 4: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, this example considers the current density to the system CO2The effect of the absorption effect.\|[0042] Experiment researches electrochemical CO2The capture and mineralization sealing system has different current densities of 0.5 mA-cm-2～6mA·cm-2For CO in air when silicate A is contained2The absorption effect of (2) is shown in FIG. 4 (a). It can be seen that as the current density increases, the mixed gas is dischargedCO2Reduced content, system to CO2The time for absorption to reach stability increases. However, the system is for CO in air2Is not proportional to the output of system power, and fig. 4(b) shows CO in the system exhaust2The concentration of (A) is varied with the system power and is 0.5mA cm-2～6mA·cm-2In the current density range, CO2The increase in processing power of (a) is accompanied by an exponential increase in system power.\|INVENTION MODE\|[0043] Example 5: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, this example compares the electrode material to the system CO2The effect of the absorption effect.\|[0044] FIG. 5(a) shows the CO content of the system in air when the anode electrode materials are copper sheet, platinum sheet, foam copper and foam nickel respectively2And (5) comparing the absorption effect. Wherein, the copper sheet and the platinum sheet are flat electrodes, and the foam copper and the foam nickel are porous electrodes. It can be seen that under the premise of the same current density, the change of the electrode material can be used for CO in the air2The absorption effect of (2) has an influence, and the system tank pressure changes remarkably. When the foam nickel with the porous structure is used as the anode, the power consumption is minimum, and the energy is saved most.\|INVENTION MODE\|[0045] Example 6: CO 22The structure of the electrochemical capture and mineralization sequestration system is the same as that of the embodiment 1, and the reaction module in the embodiment operates in a transient state and steady state combined operation mode.\|[0046] FIG. 6 shows the system pairs and CO in air for the transient and steady state combined operation mode of the reaction module2Wherein the area of the electrode used for the anode in the reaction module is 4cm2. FIG. 6(a) shows the change of the current of the reaction module with time, the system is at 6mA (1.5mA cm) in 0-5 min-2) On the basis, 2mA (0.5mA cm) is loaded-2) The frequency of the current change is 1 Hz; changing the frequency of the loading alternating current signal to 0.1Hz in the following 25 minutes; in thatThe frequency change is increased to 1000Hz in 30-55 minutes, and in the last 25 minutes, the system is in an intermittent discharge mode, namely, the system stops for 1 minute every 5 minutes of operation. FIG. 6(b) shows the system outlet CO in the operating mode as shown in FIG. 6(a)2The concentration of (c) is varied. It can be seen that in the transient and steady state combined operation mode, the system still works against CO in air2Has obvious effect on absorption.\|INVENTION MODE\|[0047] Example 7: CO 22The structure of the electrochemical capture and mineralization sequestration system is the same as that of the embodiment 1, and the embodiment considers that the system is used for CO in the air when the current is low2Absorption effect of\|[0048] FIG. 7 shows the use of 0.075mA cm in the reaction module-2System for CO in air2The absorption effect of (1). The results show that the system is in this mode of operation, after 20 minutes, towards CO2The absorption enters a stable operation state, and the CO in the air can be reduced after the absorption is stable2About 50ppm.\|INVENTION MODE\|[0049] Example 8: CO 22The structure of the electrochemical capture and mineralization sealing system is the same as that of the embodiment 1, and the embodiment considers that the system is used for high-purity CO in the operation of high current density2Absorption effect of\|[0050] FIG. 8 shows the current density of 2A cm for the reaction module-2System for high purity CO2(99.995%) absorption over time. Here, the absorption rate is defined as CO2The ratio of the change in flow rate before and after entering the system to the inlet flow rate. The results show that the system has a relatively short settling time in this mode of operation, and that 13% absorption is achieved in the 3 minute system, with the absorption increasing with time and reaching a 15% absorption efficiency after 20 minutes.	(CN106757119)\|TECHNICAL FIELD\|[0002] The invention belongs to the technical field of capture and storage of carbon resources, and relates to a method for realizing CO2Electrochemical system for capture and mineralization sequestration\|BACKGROUND ART\|[0004] CO excessively discharged in China2Mainly from fossil fuel combustion, e.g. for power generation, but also from small dispersed sources, e.g. automobile engines, and combustion in residential and commercial buildingsA furnace; in addition to this, CO2Also in the refining of certain mineral resources. Currently, excessive emission of CO2Has led to an increasingly severe greenhouse effect, due to the large part of CO2Gas is absorbed by the ocean, which makes the ocean acidification problem increasingly serious. The concern of the international society on climate change leads to the emergence of the framework convention of climate change of the united nations, and further promotes CO2Development of capture and sequestration technology (CCS) technology.\|[0005] CCS technology generally includes three major components of capture, transport and containment. First, the capture step is to capture CO2Separated from other gaseous products. Such as combustion processes in power plants, separation techniques may be employed to capture CO after combustion2Or decarbonizing the fuel prior to combustion. Secondly, in order to capture CO2Transport to CO2The source is far away from the appropriate sequestration site, requiring transportation steps to be taken. Captured CO for ease of transportation and sequestration2High concentration compression is typically performed by the capture device. Last CO2The sequestration process is the core of CCS technology, determining the overall process cost and process complexity. Currently, CO2The sealing technology comprises three types of geological sealing, ocean sealing and mineralization sealing, and the technology is greatly different from the maturity of the market. Geological sequestration technology is relatively mature, and currently, industrial demonstration projects are available, such as: the Norwegian North sea Sleipner geological sequestration project has successfully injected 1000 million tons of CO into the ground2. However, the application area of geological sequestration is limited, which is not only closely related to the formation of geological rock, but also has high cost for later monitoring and maintenance, and is easy to cause geological disasters if leakage occurs.\|[0006] Ocean sequestration and mineralization sequestration are currently only in the research, development, or demonstration stages. Among these, the mineralization sequestration technology has great potential to develop, which mainly utilizes the basic or alkaline earth oxides, such as magnesium oxide and calcium oxide, present in naturally occurring silicate rocks to sequester CO2And (5) curing. These substances are mixed with CO2Chemical reactions produce compounds such as magnesium carbonate and calcium carbonate. The advantages of mineralization and sequestration are as follows: (1) wide raw material sourceAnd 4. preparing the compound. On the one hand, the reserves of silicate rock in the crust are enormous, while these oxides may also be present in certain industrial wastes, such as stainless steel slag and mineral ash; (2) CO 22After mineralization, the mineral is not released into the atmosphere, compared with geological storage and ocean storage, the mineral is free from subsequent monitoring and maintenance cost, and the storage risk is small; (3) the mineralized carbonate product has wide application, can be used as building materials and fireproof coatings, is also an important chemical raw material, and is widely applied to the industries of chemical industry, glass, paper making and the like.\|[0007] CO presently disclosed2There are two main types of capture and mineralization sequestration techniques. One is achieved by chemical methods, while the other is based on electrochemical methods. The former is mostly carried out at high temperature or high pressure, and the system structure is complex. For example, Olsen Espen discloses the use of metal oxide salt solutions to absorb CO at temperatures between 600 ℃ and 1600 ℃2The technology and process of (CN 102448581A, US 20120128559). Terasaka et al (chem. Eng. Technol.2006, 29No 9, pp. 1118-4) Absorption of CO as a working medium2The mineralization product is Li2CO3And Li2SiO3In the form of suspended solid particles. US2005036932 discloses an absorption and removal of CO from flue gas2By bubbling the exhaust gas through a stream containing CaO and/or Ca (OH)2Of solid particles of (a) so that CO in the exhaust gas is present2Conversion to CaCO3. CN 102491795A discloses CO at 150-350 deg.C2Under the condition that the partial pressure is not lower than 1.0MPa, the potassium feldspar is used for leading CO to be treated2A method for producing a potassium-rich solution by mineralization; CN 102895847A discloses that CO is introduced into2The trapping method comprises introducing molten alkali metal, alkaline earth metal, transition metal carbonate, silicate, borate, oxide, hydroxide, nitrate, aluminate and their mixture into the reactor for absorption electrolysis. CN 103111161A discloses a larger scale CO2Capture process by CO with positive pressure2Solvent capture of CO in a capture column2Supersaturated CO2The solution enters a releasing tower again for extraction and concentration.CO based electrochemical process2The capture and conversion process is relatively simple and the operating environment is relatively mild, CN 101670236A discloses recovery of CO by aqueous carbonate capture and electrodialysis2By aqueous solution capture of CO2Subsequent electrodialysis to form CO-rich2Liquid flow and regenerated capture solution. CN 102351310A discloses microbial electrochemical CO2A capture system using organic wastewater as a microbial nutrient source in CO2The problem of sewage treatment is considered while the sewage is captured. CN 102978653A discloses a mineralized CO2The membrane electrolysis method for coproducing strong acid is characterized by that its mineralized raw material is nitrate or sulfate, and its product is carbonate and nitric acid. CN 105420751 a discloses a method for preparing hydrocarbons by electrochemical reduction of carbon dioxide, which uses alkali metal carbonate (bicarbonate), sulfate, phosphate (bicarbonate), etc. as substances and electrolyte, and is characterized in that an organic solvent is introduced into an electrolyte system. Unlike electrochemical capture in aqueous systems, CN 103590064 a discloses the use of anhydrous LiF and Li2CO3The molar ratio (0.5-1.5): 1, uniformly mixing, adding an additive to prepare electrolyte molten salt, placing the electrolyte molten salt in an electrolytic cell, heating to 690-700 ℃, and introducing CO2An electrolytic capture method. Wherein the cathode material is Ni or Ti, and the anode material is Pt, Fe-Ni alloy or Fe-Ni-Al2O3And (3) alloying.\|DISCLOSURE\|[0008] Disclosure of Invention\|[0009] In order to overcome the defects in the prior art, the invention provides a method for realizing CO2An electrochemical system for capturing, mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed; the liquid flow discharged after the system is operated is alkaline, and the treatment of ocean acidification problems in a designated area can be realized to a certain extent.\|[0010] Can realize CO2The technical scheme of the electrochemical system for capturing, mineralizing and sealing up comprises the following steps:\|[0011] the system comprises a fluid power module, a reaction module and a control and display module, wherein the fluid power module is connected with the reaction module and provides CO for the reaction module2The feed gas and the supplementary electrolyte and the reactant of (1); the reaction module is CO2The capture and mineralization sealing provides a reaction site, which comprises an anode chamber, a cathode chamber and a diaphragm; the anode chamber is internally provided with an electrode, electrolyte, silicate and/or mineral containing silicate, and the cathode chamber is internally provided with an electrode and electrolyte; the anode chamber is separated from the cathode chamber by a diaphragm; the control and display module is simultaneously connected with the reaction module and the fluid power module, provides running electric power for the fluid power module, and simultaneously realizes a steady state or transient state and steady state combined electrochemical reaction mode for the reaction module, so that silicate is converted into carbonate, and CO is realized2Capture and mineralize and seal up.\|[0012] The diaphragm in the reaction module comprises an anion-exchange membrane, a cation-exchange membrane or a microporous membrane (such as a porous polytetrafluoroethylene membrane); the electrode material comprises simple substances, alloys or compounds formed by other nonmetal elements containing Pt, Re, Pd, Rh, Mo, Wo, Nb, Ru, Ir, Sn, Mn, Fe, Co, Ni, Cu, Ag and C. The silicate includes all compounds or mixtures containing silicon, oxygen and other chemical elements (such as aluminum, iron, calcium, magnesium, manganese, potassium, sodium, barium, copper, zinc, lead, tin). The silicate-containing mineral includes olivine, serpentine, basalt, asbestos, mica, talc, kaolinite, montmorillonite, zeolite, agalmatolite, tourmaline, pyroxene, and hornblende containing the above silicate components.\|[0013] The anode is of a flat electrode structure or a porous electrode structure.\|[0014] CO treated in the anode chamber2The concentration range of the mixed gas is between 0.050% and 99.995%.\|[0015] When the operation mode of the reaction module is steady state, the working current density range is 0.075mA/cm2～2 A/cm2To (c) to (d); when the operation mode of the reaction module is transient, a sine wave, a square wave and a three wave of current or voltage are loaded on the systemThe angular wave signal has a variation frequency range of 1000 Hz-0.1 Hz.\|[0016] The control and display module comprises a sensing device, a system control device and a display device; wherein the sensing device comprises H2、O2、CO2A concentration sensor, a temperature sensor, a liquid level sensor and a pressure sensor; the display device is used for displaying temperature, pressure and O in system operation2Concentration, H2Concentration, CO2Concentration, level, current, voltage information; on one hand, the system control device provides electric power for the sensing device and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a digital signal processor in the system control device controls the operation of the reactor, and provides a steady-state operation mode, a transient-state operation mode or a steady-state and transient-state combined operation mode for the system.\|[0017] CO of system treatment2The concentration range of the gas is wide, namely high-concentration CO can be realized2(99.99%) conversion can also be used for trace amounts of CO in air2(ppm level) conversion, System CO2The transformation scale of (2) is controllable and modularization is easy to realize. The discharged product of the system after operation is environment-friendly and alkaline, and the system can realize CO2The problem of ocean acidification which is becoming more serious at present can be simultaneously relieved while the capture and the mineralization are sealed.\|[0018] The invention realizes CO by adopting an electrochemical method2Compared with the application of physical methods (including geological storage and ocean storage), the technology does not need to be monitored in the later period and has no risk of geological disasters. Compared with the existing applied chemical method to realize CO2Compared with the technology of capture and mineralization sealing, the invention applies the electrochemical method without high temperature and high pressure reaction environment, the reaction can be carried out at normal temperature and normal pressure, the system has simple structure and low energy consumption, and is easy to realize modular design and has huge application prospect.\|DRAWINGS DESCRIPTION\|[0020] FIG. 1 is CO2The structure of the electrochemical capture and mineralization sealing system is shown schematically.\|[0021] FIG. 2 is introduction of calcium silicate to CO in air2The absorption efficiency and the system cell pressure.\|[0022] FIG. 3 is a graph of silicate species vs. CO in the air of the system2The effect of the absorption effect of (c).\|[0023] FIG. 4 is a graph of the system versus CO in air at different current densities2The absorption effect of (1).\|[0024] Wherein (a) is CO2A time-dependent profile; (b) after 3 hours, CO2Concentration profile with system power.\|[0025] FIG. 5 shows 4mA cm of electrode material at room temperature for a system-2For CO in air under the condition2The effect of absorption.\|[0026] Wherein (a) is CO2The change in concentration over time; (b) is the change of the system tank pressure with time.\|[0027] FIG. 6 shows the system operating under unsteady state current conditions for CO in air2The absorption effect of (1).\|[0028] Wherein (a) is the variation of the system current with time; (b) is CO2The change in concentration with time.\|[0029] FIG. 7 is a graph of the system versus CO in air at low current density2The absorption effect of (1).\|[0030] FIG. 8 is a graph of system for high purity CO at high current density2The absorption effect of (1).\|INVENTION MODE\|[0031] Detailed Description\|[0032] To further illustrate the invention, the following examples are presented to describe CO2The electrochemical capture and containment system is not intended to limit the scope of the invention.\|INVENTION MODE\|[0033] Example 1: CO 22Electrochemical capture and containment system architecture\|[0034] FIG. 1 shows CO2And (3) an electrochemical capture and mineralization sequestration system structure. The system consists of a fluid power module, a reaction module and a control and display module. The fluid power module is connected with the reaction module and can be provided with CO2May also be supplemented with supporting electrolytes and reactants. The control and display module is simultaneously connected with the reaction module and the fluid power module, and the system controller provides electric power for the sensing device on one hand and controls the fluid power module to provide reactants and supplement electrolyte for the reactor according to the response of the sensing device; on the other hand, a Digital Signal Processor (DSP) in the controller can control the operation of the reactor, provide steady-state, transient-state, steady-state and transient-state combined operation modes for the system and realize shutdown operation. The reaction module is the core component of the system and is CO2The capture and mineralization sealing provides a reaction site, and the structure of the device consists of an anode chamber, a cathode chamber and a diaphragm. The anode chamber and the cathode chamber are respectively provided with an anode, an anolyte, a cathode and a catholyte, wherein the anode chamber contains silicate.\|INVENTION MODE\|[0035] Example 2: CO 22The electrochemical capture and mineralization sequestration system is the same as example 1, which compares the addition or non-addition of silicate to the system CO2Absorption efficiency and emission of products.\|[0036] FIG. 2 shows electrochemical CO with and without silicate minerals2A capture and mineralization sealing system with a current density of 2mA cm-2Under the condition, the system can be used for treating CO in the air2The absorption effect and the system tank pressure. It can be seen that the introduction of calcium silicate is for CO2The absorption and system power consumption effects of (1) produced significant results after 100 minutes, calcium silicate containing system exhaust gas CO2The concentration is relatively low. Table 1 shows the effect of silicate incorporation on the pH of the effluent after 8 hours of operation of the system, which is seen in calcium silicate incorporationThe acidification degree of the anode discharge product is obviously reduced.\|[0037] TABLE 1 Effect of silicate incorporation on the pH of the anode and cathode compartments\|[0038] \|INVENTION MODE\|[0039] Example 3: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, in this example, silicate species are compared to system CO2The absorption efficiency of (a).\|[0040] FIG. 3 shows the reaction at CO2After calcium silicate, magnesium silicate, aluminum silicate and sodium silicate are introduced into the electrochemical capture and mineralization sealing system, the system can be used for treating CO in the air at room temperature2Comparison of absorption effects. The reaction module is operated in a steady-state constant current mode in the system operation, and the current is 2 mA-cm-2. It can be seen that the type of silicate affects the system CO2Transient and steady state behavior of the absorption. System Pair CO introducing aluminum silicate and magnesium silicate 1 hour after system startup2The absorption effect is inferior to that of the system containing calcium silicate and sodium silicate. After 3 hours of operation, the system had entered steady state, with systems employing magnesium silicate for CO2The absorption effect of (A) is inferior to that of the other three silicates.\|INVENTION MODE\|[0041] Example 4: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, this example considers the current density to the system CO2The effect of the absorption effect.\|[0042] Experiment researches electrochemical CO2The capture and mineralization sealing system has different current densities of 0.5 mA-cm-2～6mA·cm-2For CO in air when silicate A is contained2The absorption effect of (2) is shown in FIG. 4 (a). It can be seen that as the current density increases, the mixed gas is dischargedCO2Reduced content, system to CO2The time for absorption to reach stability increases. However, the system is for CO in air2Is not proportional to the output of system power, and fig. 4(b) shows CO in the system exhaust2The concentration of (A) is varied with the system power and is 0.5mA cm-2～6mA·cm-2In the current density range, CO2The increase in processing power of (a) is accompanied by an exponential increase in system power.\|INVENTION MODE\|[0043] Example 5: CO 22The electrochemical capture and mineralization sequestration system structure is the same as example 1, this example compares the electrode material to the system CO2The effect of the absorption effect.\|[0044] FIG. 5(a) shows the CO content of the system in air when the anode electrode materials are copper sheet, platinum sheet, foam copper and foam nickel respectively2And (5) comparing the absorption effect. Wherein, the copper sheet and the platinum sheet are flat electrodes, and the foam copper and the foam nickel are porous electrodes. It can be seen that under the premise of the same current density, the change of the electrode material can be used for CO in the air2The absorption effect of (2) has an influence, and the system tank pressure changes remarkably. When the foam nickel with the porous structure is used as the anode, the power consumption is minimum, and the energy is saved most.\|INVENTION MODE\|[0045] Example 6: CO 22The structure of the electrochemical capture and mineralization sequestration system is the same as that of the embodiment 1, and the reaction module in the embodiment operates in a transient state and steady state combined operation mode.\|[0046] FIG. 6 shows the system pairs and CO in air for the transient and steady state combined operation mode of the reaction module2Wherein the area of the electrode used for the anode in the reaction module is 4cm2. FIG. 6(a) shows the change of the current of the reaction module with time, the system is at 6mA (1.5mA cm) in 0-5 min-2) On the basis, 2mA (0.5mA cm) is loaded-2) The frequency of the current change is 1 Hz; changing the frequency of the loading alternating current signal to 0.1Hz in the following 25 minutes; in thatThe frequency change is increased to 1000Hz in 30-55 minutes, and in the last 25 minutes, the system is in an intermittent discharge mode, namely, the system stops for 1 minute every 5 minutes of operation. FIG. 6(b) shows the system outlet CO in the operating mode as shown in FIG. 6(a)2The concentration of (c) is varied. It can be seen that in the transient and steady state combined operation mode, the system still works against CO in air2Has obvious effect on absorption.\|INVENTION MODE\|[0047] Example 7: CO 22The structure of the electrochemical capture and mineralization sequestration system is the same as that of the embodiment 1, and the embodiment considers that the system is used for CO in the air when the current is low2Absorption effect of\|[0048] FIG. 7 shows the use of 0.075mA cm in the reaction module-2System for CO in air2The absorption effect of (1). The results show that the system is in this mode of operation, after 20 minutes, towards CO2The absorption enters a stable operation state, and the CO in the air can be reduced after the absorption is stable2About 50ppm.\|INVENTION MODE\|[0049] Example 8: CO 22The structure of the electrochemical capture and mineralization sealing system is the same as that of the embodiment 1, and the embodiment considers that the system is used for high-purity CO in the operation of high current density2Absorption effect of\|[0050] FIG. 8 shows the current density of 2A cm for the reaction module-2System for high purity CO2(99.995%) absorption over time. Here, the absorption rate is defined as CO2The ratio of the change in flow rate before and after entering the system to the inlet flow rate. The results show that the system has a relatively short settling time in this mode of operation, and that 13% absorption is achieved in the 3 minute system, with the absorption increasing with time and reaching a 15% absorption efficiency after 20 minutes.	Family Number\|(76279049)\|76279049\|Object of Invention\|(CN106757119B B)\|In order to overcome the defects in the prior art , the invention provides a method for realizing CO2An electrochemical system for capturing , mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed ; the liquid flow discharged after the system is operated is alkaline , and the ( . . . ) \|(CN106757119 A)\|In order to overcome the defects in the prior art , the invention provides a method for realizing CO2An electrochemical system for capturing , mineralizing and sealing the silicate or the silicate rock existing in the natural ore such as serpentine and olivine is used to convert it to carbonate by electrochemical method to realize CO2The mineralization is sealed ; the liquid flow discharged after the system is operated is alkaline , and the ( . . . ) \|Abstract\|(CN106757119B B)\|The invention belongs to the technical field of carbon resource capturing and storing and relates to a system for achieving CO2 capturing and mineralization through an electrochemical method . The system is structurally composed of three parts of a hydrodynamic force module , a reaction module and a control and display module . By means of the electrochemical technology of a steady state , a transient state and combination of the steady state and the transient state , silicate is converted into carbonate , and CO2 capturing and mineralization are achieved . The CO2 capturing and mineralization system is mainly used for relieving the increasing greenhouse effect , liquid flow drained by the system is alkaline , and treatment of ocean acidification of local areas is achieved at the same time . The system can also be used for adjusting the concentration of CO2 gas in a closed space in real time and can also serve as an auxiliary facility for emission reduction of large CO2 emission enterprises . \|	Surface technology, coating	C25B-001/00\|C25B-015/02\|Y02C-020/40		C25B-001/00\|C25B-015/02\|Y02C-020/40	C25B-001/00\|C25B-015/02	C25B-001/00\|C25B-015/02			CN109855206\|CN117023729B\|CN117233253B	CN109855206 84771358 WHO=Examiner SELF=N CAT=A\|CN117023729B 107214603 WHO=Examiner SELF=N\|CN117233253B 107757227 WHO=Examiner SELF=N	CN102899679\|CN101134155\|KR20160119429\|CN104477950\|CN103966622\|US20140238871\|US9464010\|CN103230735\|CN103173782\|CN102978653\|CN102895847\|CN102762277\|CN101878060\|JP2010125354	CN102899679 8151397 WHO=Examiner SELF=N CAT=Y\|CN101134155 6409477 WHO=Examiner SELF=N CAT=Y\|KR20160119429 74446448 WHO=Examiner SELF=N CAT=A\|CN104477950 68955167 WHO=Examiner SELF=N CAT=A\|CN103966622 67167903 WHO=Examiner SELF=N CAT=A\|US20140238871 1895012 WHO=Examiner SELF=N CAT=A\|US9464010 65403965 WHO=Examiner SELF=N CAT=A\|CN103230735 45750692 WHO=Examiner SELF=N CAT=A\|CN103173782 45517523 WHO=Examiner SELF=N CAT=A\|CN102978653 8171552 WHO=Examiner SELF=N CAT=A\|CN102895847 8135679 WHO=Examiner SELF=N CAT=A\|CN102762277 1910468 WHO=Examiner SELF=N CAT=A\|CN101878060 6949869 WHO=Examiner SELF=N CAT=A\|JP2010125354 33126904 WHO=Examiner SELF=N CAT=A	理查德•A•斯科特等: "《防护用纺织品》", 31 March 2016, 中国纺织出版社 (Cat. A)	CN101134155; CN103966622; CN103230735; CN101878060; CN102762277; CN103173782; CN102895847; CN102978653; CN104477950; US20140238871; JP2010125354; KR20160119429; US9464010; CN102899679		GRANTED	(CN106757119)\|GRANTED	ALIVE	(CN106757119)\|ALIVE	(CN106757119)\|LEGAL DETAILS FOR CN106757119\|Actual or expected expiration date=2036-12-09\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2016-12-09\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201611128528\|Application date=2016-12-09\|Standardized application number=2016CN-1128528\|Event publication date=2017-05-31\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN106757119\|Publication stage code=A\|Publication date=2017-05-31\|Standardized publication number=CN106757119\|Event publication date=2017-05-31\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2017-06-23\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2019-02-26\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN106757119\|Publication stage code=B\|Publication date=2019-02-26\|Standardized publication number=CN106757119B\|Event publication date=2019-02-26\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right		(CN106757119)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjn+frZymVg1jxj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000022549569&ekey=1953&xpn=CN106757119B&kind=B	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=kWAwQSdm5YD2iOc1MipqmrmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN106757119)\|CN\|(CN106757119)\|CN	(CN106757119)\|NAME=DALIAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN\|(CN106757119)\|NAME=DALIAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN		(CN106757119)\|NAME=MEI HONGYU;PATENT AGENCY CENTER OF DLUT , REG=21200\|(CN106757119)\|NAME=MEI HONGYU;PATENT AGENCY CENTER OF DLUT , REG=21200		(CN106757119)\|NAME=MAO QING\|NAME=CUI JIANMING\|NAME=HUANG YANQIANG\|NAME=LIU JIANJUN\|NAME=JING WEIYUN\|NAME=SHI YUE\|(CN106757119)\|NAME=MAO QING\|NAME=CUI JIANMING\|NAME=HUANG YANQIANG\|NAME=LIU JIANJUN\|NAME=JING WEIYUN\|NAME=SHI YUE	(CN106757119)\|8	1	1					(CN106757119)\|Gazette date: GAZDATE=2019-02-26\|Gazette number: GAZNUM=35-0901\|Number of Pages: NPAGES=13\|Primary examiner: 刘燕\|Primary examiner: Liu Yan\|\|(CN106757119)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2017-05-31\|Gazette number: GAZNUM=33-2201\|Number of Pages: NPAGES=13\|Primary examiner: 刘燕\|Primary examiner: Liu Yan\|		(CN106757119)\|CHINESE (CHI)	(CN106757119B)\|Patent\|(CN106757119)\|Patent	Titre: (CN106757119)\|One kind is for realizing CO2The electro-chemical systems that capture is sealed up for safekeeping with mineralising Résumé: (CN106757119)\|The invention belongs to the technical field of carbon resource capturing and storing and relates to a system for achieving CO2 capturing and mineralization through an electrochemical method. The system is structurally composed of three parts of a hydrodynamic force module, a reaction module and a control and display module. By means of the electrochemical technology of a steady state, a transient state and combination of the steady state and the transient state, silicate is converted into carbonate, and CO2 capturing and mineralization are achieved. The CO2 capturing and mineralization system is mainly used for relieving the increasing greenhouse effect, liquid flow drained by the system is alkaline, and treatment of ocean acidification of local areas is achieved at the same time. The system can also be used for adjusting the concentration of CO2 gas in a closed space in real time and can also serve as an auxiliary facility for emission reduction of large CO2 emission enterprises.	28	Abstract	gpt-4o-mini	yes	The article describes a system that uses electrochemical methods to capture CO2 and convert silicates into carbonates, which aligns with the topic of enhanced weathering and carbon sequestration.
31	CN202410297703	CN202410297703	CN118189424	110191082	CN118189424 A 2024-06-14 [CN118189424]	2024-03-15	2024-03-15	2024-06-14		(CN118189424)\|2044-03-15	(CN118189424)\|Method for generating terrestrial heat and extracting valuable elements by permanently sealing carbon dioxide through geological rock under assistance of ammonium bisulfate	(CN118189424)\|The invention discloses a method for generating terrestrial heat and extracting valuable elements by permanently sealing and storing carbon dioxide through geological rocks under the assistance of ammonium bisulfate. The method comprises the following steps that under the assistance of ammonium bisulfate, silicate rock minerals containing magnesium, calcium and iron in a geologic structure react with injected carbon dioxide, carbon dioxide is permanently sealed, meanwhile, terrestrial heat is generated, and valuable elements rich in leachate silicate are recycled. According to the method, under the assistance of ammonium bisulfate, injected carbon dioxide mixed liquid reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is rapidly generated, the mineralization fixing process is fast, meanwhile, heat release and the reaction rate are coupled to improve the geothermal grade, the reaction is accelerated through ammonium bisulfate, the mineralization reaction rate is increased, and the mineralization effect is improved. The heat release process of the mineral carbonization reaction is coupled with the reaction rate to improve the geothermal grade.	GUANGZHOU INSTITUTE OF ENERGY CONVERSION - CHINESE ACADEMY OF SCIENCES	(CN118189424)\|GUANGZHOU INSTITUTE OF ENERGY CONVERSION CHINESE ACADEMY OF SCIENCES ([CN])	CAO YAN	(CN118189424)\|CAO YAN	(CN118189424)\|FANG YAN;GUANGZHOU KEYUE I.P. LAW OFFICE\|Reg. Nb: 44001\|MO YAOJIANG;GUANGZHOU KEYUE I.P. LAW OFFICE\|Reg. Nb: 44001	(CN118189424)\|Compared with the prior art, the invention has the following advantages:\|The invention applied by the inventor realizes permanent fixation by utilizing the reaction of silicate minerals rich in magnesium, calcium and iron in geological strata and CO 2, but the risk of leakage of CO 2 back to the atmosphere can be greatly reduced and heat release is also accompanied; however, this process is very slow, and it is difficult and long time to accumulate valuable heat energy for use under the heat dissipation conditions of the geological structure, and the geological sequestration depth of CO 2 is generally better in the range of 2000-3000 meters, and this depth brings about thresholds such as drilling cost, compression energy consumption of CO 2, and the like.\|	(CN118189424)\|1. A method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which is characterized by comprising the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid.\|	(CN118189424)\|Aiming at the problems existing in the prior art, the invention provides a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide assisted by ammonium bisulfate, which can obviously accelerate the carbonization reaction path of minerals in stratum, accelerate heat release by faster reaction, drive considerable temperature rise of the rock and improve geothermal grade and economic benefit feasibility of heat collection. The invention aims to provide a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which comprises the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid. The invention discloses a carbonization reaction path capable of remarkably accelerating minerals in a stratum, accelerating heat release by faster reaction, driving considerable temperature rise of rock, and improving geothermal grade and economic benefit feasibility of heat collection.\|The invention discloses a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate.\|The invention relates to the technical field of carbon dioxide sequestration, in particular to a method for generating geothermal heat and extracting valuable elements by permanently sequestering carbon dioxide by using geological rock with the aid of ammonium bisulfate.\|	(CN118189424)\|CARBON DIOXIDE(100,41)\|AMMONIUM BISULFATE(100,38)\|GEOLOGICAL ROCK(100,12)\|GEOTHERMAL HEAT GENERATION(100,9)\|SEAL CARBON DIOXIDE(100,4)\|STORE CARBON DIOXIDE(100,1)\|GEOTHERMAL GRADE(74,17)\|ECONOMIC BENEFIT FEASIBILITY(69,2)\|GEOLOGICAL SEQUESTRATION DEPTH(61,1)\|AMMONIUM BISULFATE ASSISTANCE(59,9)\|LEACHING LIQUID(41,3)\|MINERAL ACCELERATION(38,1)\|SILICATE MINERAL(37,12)\|CARBONIZATION REACTION PATH(37,2)\|SILICATE GEOLOGICAL MINERAL(35,4)\|MINERAL CARBONIZATION REACTION PATH(31,1)\|GEOLOGY INDIRECT CARBONIZATION(30,8)\|FAST REACTION(29,2)\|PERMANENT FIXATION(29,2)\|SILICATE(28,6)\|AMMONIUM BISULFATE AID(28,1)\|GEOLOGICAL STRUCTURE(27,7)\|HEAT COLLECTING(27,2)\|STRATUM PERMEABILITY(25,4)\|STRATUM POROSITY(25,4)\|STRATUM(24,3)\|ACCELERATING HEAT(23,1)\|GEOTHERMAL HEAT(20,5)\|STRATUM MINERAL VOLUME(19,4)\|CARBON DIOXIDE SEQUESTRATION(19,3)\|UNDERGROUND DEPTH(18,5)\|GEOLOGICAL STRATA(18,2)\|TEMPERATURE GEOTHERMAL GRADE(18,2)\|COBALT RICH(17,4)\|DRILLING COST(17,2)\|SEQUESTERING CARBON DIOXIDE(17,1)\|GEOLOGICAL MINERAL CARBONIZATION(15,2)\|COMPRESSION ENERGY CONSUMPTION(13,2)\|WOLLASTONITE(13,2)\|VALUABLE HEAT ENERGY(13,1)\|FLUID MIXING(12,7)\|ANORTHITE(12,2)\|SEEPAGE(11,6)\|STRATUM TEMPERATURE(11,4)\|BASALT(11,2)\|HEAT DISSIPATION(11,1)\|GEOLOGY DIRECT CARBONIZATION(10,3)\|MINERALIZATION REACTION RATE(9,4)\|SEALING CARBON DIOXIDE(9,2)\|FORMATION CONDITION(8,4)\|ENERGY CONSUMPTION(8,2)\|GEOLOGICALLY DIRECT CARBONIZATION(8,2)\|MEDIUM TEMPERATURE(8,2)\|ASSISTED PERMANENT SEQUESTRATION(8,1)\|GEOLOGICAL INDIRECT CARBONIZATION FEATURE(8,1)\|OLIVINE MAGNESIUM EXTRACTION EXPERIMENT(8,1)\|TEMPERATURE RISE(7,9)\|STRATUM FLOW PRESSURE(7,4)\|ANNUAL CARBON SEQUESTRATION(7,3)\|OLIVINE SAMPLE(7,3)\|SHALLOW OLIVINE(7,2)\|SIMULTANEOUSLY COUPLING HEAT RELEASE(7,2)\|ELECTRON MICROSCOPIC CRACK GRAPH(7,1)\|GEOLOGICAL SEQUESTRATION(7,1)\|STRATUM CONDITION(6,4)\|CHINA ECONOMIC BENEFIT(6,1)\|GEOLOGICAL ROCK STRATUM(6,1)\|OLIVINE FLAKE(6,1)\|OLIVINE TON(6,1)\|SEALING GEOLOGICAL GRADE(6,1)\|CARBON DIOXIDE MIXED SOLUTION(5,4)\|DRILLING SEALING(5,2)\|LEACHING SOLUTION IRON SILICATE(5,2)\|RECYCLING POTENTIAL(5,2)\|UNTREATED SAMPLE(5,2)\|CARBONATION CAPACITY(5,1)\|CHRYSOTILE MG(5,1)\|COBALT PRODUCTIVITY(5,1)\|DIFFICULT TIME(5,1)\|ELEMENTAL SCAN SPECTRUM(5,1)\|EXTRACTABLE NICKEL(5,1)\|MAGNESIUM CALCIUM SILICATE ROCK(5,1)\|MAGNESIUM ELEMENTAL DISTRIBUTION(5,1)\|MINERAL CARBONIZATION MODE(5,1)\|OLIVINE MINERAL(5,1)\|SEALING GEOLOGICAL DEPTH(5,1)\|TREND ASCENSION(5,1)\|AVERAGE OLIVINE TEMPERATURE RISE(4,7)\|CARBON DIOXIDE PRESSURE(4,6)\|MASS TRANSFER(4,6)\|REACTION MATURATION TIME(4,6)\|INJECTION CONDITION(4,4)\|BOX BENHNKEN(4,1)\|COBALT NICKEL EXTRACTION(4,1)\|CORE SEM CRACK DIAGRAM(4,1)\|CORE SLICE(4,1)\|DEVELOPMENT RESOURCE(4,1)\|GEOLOGICAL SEALING(4,1)\|GEOLOGICALLY INDIRECT CARBONIZATION RESULT(4,1)\|GEOTHERMAL ENERGY BENEFIT(4,1)\|LOGARITHMIC RELATIONSHIP(4,1)\|OLIVE STRATA TEMPERATURE(4,1)\|OLIVINE MG(4,1)\|SMELTING BENEFIT(4,1)\|SQUARE KILOMETER FOREST(4,1)\|STEAM COLLECTION(4,1)\|REACTION TEMPERATURE(3,4)\|BRUCITE(3,2)\|IRON CONTENT(3,2)\|SEM TEST(3,2)\|STABLE CARBONATE(3,2)\|WEAK ALKALI SALT(3,2)\|ANNUAL CARBON STORAGE(3,1)\|BRINE LAYER DEPTH(3,1)\|CARBON NEUTRALIZATION(3,1)\|COBALT CAPACITY(3,1)\|CRACK DEPTH(3,1)\|DRY HOT ROCK(3,1)\|EXPERIMENTAL FACTOR(3,1)\|EXTRACTING MG(3,1)\|FACTOR INTERACTION(3,1)\|FORMATION PERMEABILITY(3,1)\|FORMATION POROSITY(3,1)\|GEOLOGICAL DIRECT CARBONIZATION TEMPERATURE(3,1)\|GEOLOGICAL STORAGE(3,1)\|GEOLOGY INDIRECT CARBONIZATION RESULT(3,1)\|KG YEAR(3,1)\|PRESSURIZED INJECTION(3,1)\|REACTION ACCELERATOR(3,1)\|REACTION PROGRESSION(3,1)\|RECOVERING NICKEL(3,1)\|ROCK SAMPLE(3,1)\|SILICATE MINERAL PROPOSITION(3,1)\|	(CN118189424)\|1. A method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which is characterized by comprising the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid.\|2. The method according to claim 1, characterized in that it comprises in particular the following steps: injecting a mixed fluid of ammonium bisulfate and carbon dioxide into a stratum of silicate minerals containing magnesium, calcium and iron, reacting the mixed fluid with the silicate minerals containing magnesium, calcium and iron to generate carbonate, permanently sealing carbon dioxide, simultaneously coupling heat release and reaction rate to improve geothermal grade, and recovering valuable elements nickel and cobalt rich in silicate in the leaching solution.\|3. The method of claim 2, wherein the formation conditions comprise: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3.\|4. The method of claim 2, wherein the injection conditions of the mixed fluid of ammonium bisulfate and carbon dioxide comprise: the temperature of the mixed fluid is 20-200 ℃, the pressure of carbon dioxide is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection.\|5. The method of claim 2, wherein the geothermal grade is a medium and high temperature geothermal grade greater than 150 ℃.\|6. A method according to claim 1 or 2, wherein the silicate minerals comprise olivine, serpentine, basalt, wollastonite and anorthite which are rich in magnesium, calcium and iron.\|7. The method according to claim 1 or 2, wherein the concentration of NH 4HSO4 in the mixed fluid is 0.1-2.0mol/L and the solid-to-liquid ratio of silicate mineral to NH 4HSO4 solution is 100-1000kg/L.\|8. Use of the method of claim 1 or 2 for sequestering carbon dioxide.	(CN118189424)\|TECHNICAL FIELD\|[0001] The invention relates to the technical field of carbon dioxide sequestration, in particular to a method for generating geothermal heat and extracting valuable elements by permanently sequestering carbon dioxide by using geological rock with the aid of ammonium bisulfate. \|BACKGROUND ART\|The background technology is as follows:\|[0002] large scale carbon capture, utilization and sequestration (CCUS) technologies must be developed to achieve carbon neutralization, which involves injection of CO 2 into geological structures, such as deep brine layers or Enhanced Oil Recovery (EOR) in oil fields, but may involve leakage of freely stored CO 2 back to the atmosphere. \|[0003] The invention applied by the inventor realizes permanent fixation by utilizing the reaction of silicate minerals rich in magnesium, calcium and iron in geological strata and CO 2, but the risk of leakage of CO 2 back to the atmosphere can be greatly reduced and heat release is also accompanied; however, this process is very slow, and it is difficult and long time to accumulate valuable heat energy for use under the heat dissipation conditions of the geological structure, and the geological sequestration depth of CO 2 is generally better in the range of 2000-3000 meters, and this depth brings about thresholds such as drilling cost, compression energy consumption of CO 2, and the like.\|[0004] In view of the fact that geothermal energy has become one of the most competitive renewable energy utilization modes, the CO 2 geological sequestration is indeed capable of generating geothermal-like heat for utilization, and a new method is needed to achieve carbon dioxide sequestration while improving geothermal grade.\|DISCLOSURE\|The invention comprises the following steps:\|[0005] Aiming at the problems existing in the prior art, the invention provides a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide assisted by ammonium bisulfate, which can obviously accelerate the carbonization reaction path of minerals in stratum, accelerate heat release by faster reaction, drive considerable temperature rise of the rock and improve geothermal grade and economic benefit feasibility of heat collection. \|[0006] The invention aims to provide a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which comprises the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid.\|[0007] The invention discloses a carbonization reaction path capable of remarkably accelerating minerals in a stratum, accelerating heat release by faster reaction, driving considerable temperature rise of rock, and improving geothermal grade and economic benefit feasibility of heat collection. According to the invention, strong acid weak alkali salt (ammonium bisulfate NH 4HSO4) is adopted to accelerate the reaction of magnesium calcium silicate in a geological structure and injected CO 2, NH 4HSO4 has the potential of recycling, nickel and cobalt high-value elements rich in magnesium, calcium and iron silicate in leaching liquid are recovered, the nickel and cobalt productivity is improved to meet the requirements of clean energy sources of electric automobiles, the carbon footprint in mining activities is reduced, and high-purity amorphous silicon dioxide and brucite produced by subsequent processing of the solution can also be used for other chemical production.\|[0008] The method provided by the invention is characterized in that under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade.\|[0009] Preferably, the method specifically comprises the following steps: injecting a mixed fluid of ammonium bisulfate and carbon dioxide into a stratum of silicate minerals containing magnesium, calcium and iron, reacting the mixed fluid with the silicate minerals containing magnesium, calcium and iron to generate carbonate, permanently sealing carbon dioxide, simultaneously coupling heat release and reaction rate to improve geothermal grade, and recovering valuable elements nickel and cobalt rich in silicate in the leaching solution.\|[0010] The method provided by the invention is to inject the mixed fluid of CO 2 and ammonium bisulfate into a well, seal the well, open the well after the reaction is mature, collect steam and nickel-cobalt solution, realize that geological rock permanently seals carbon dioxide to generate geothermal heat and extract valuable elements nickel-cobalt.\|[0011] The invention continuously pushes the proposed silicate minerals which are rich in magnesium, calcium and iron in geological strata to react with CO 2 to realize permanent fixation technology, adopts strong acid weak alkali salt (such as ammonium bisulfate NH 4HSO4), accelerates the reaction of magnesium calcium silicate rock in geological structures with injected CO 2, and NH 4HSO4 has recoverable recycling potential, simultaneously recovers nickel and cobalt high-value elements which are rich in magnesium, calcium and iron silicate in leaching solution, improves the nickel and cobalt capacity to meet the requirements of clean energy of electric vehicles, reduces the carbon footprint in mining activities, ensures that the high-purity amorphous silicon dioxide and brucite which are produced by subsequent processing of the solution can also be used for other chemical production, changes the defect of very slow conventional permanent sealing reaction rate, improves the sealing geological grade, simultaneously reduces the sealing geological depth, and obtains high-value elements including recovered nickel and cobalt, reduces the cost, the compression energy consumption of CO 2 and the like.\|[0012] Preferably, the formation conditions include: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3. Different injection conditions and stratum conditions bring different geological mineral carbonization effects, and corresponding injection conditions are selected under different stratum conditions, so that the energy utilization rate is improved. Further preferably, the formation conditions include: the underground depth is 1000-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3.\|[0013] Preferably, the injection conditions of the mixed fluid of ammonium bisulfate and carbon dioxide comprise: the temperature of the mixed fluid is 20-200 ℃, the pressure of carbon dioxide is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection.\|[0014] Preferably, the geothermal grade is a medium and high temperature geothermal grade greater than 150 ℃.\|[0015] Preferably, the silicate minerals include olivine, serpentine, basalt, wollastonite and anorthite which are rich in magnesium, calcium and iron.\|[0016] Preferably, the concentration of NH 4HSO4 in the mixed fluid is 0.1-2.0mol/L, the solid-to-liquid ratio of silicate mineral to NH 4HSO4 solution is 100-1000kg/L, and the reaction temperature is 50-180 ℃.\|[0017] The invention also protects the application of the method in carbon dioxide sequestration.\|[0018] Compared with the prior art, the invention has the following advantages:\|[0019] 1. According to the method provided by the invention, in the geological rock and 2-year period, the initial temperature of the related geological rock stratum and the temperature of the CO 2 fluid injected are 37 ℃ and 1 cubic kilometer, the average temperature rise of the rock can reach 105 ℃ and reach 142 ℃ at the final temperature, high geothermal grade reaction heat is generated, and meanwhile, the geological storage CO 2 amount can reach 11.9 ten thousand tons each year, which is equivalent to the annual carbon storage amount of 342k square kilometer forests in northwest China; if the temperature of the fluid injected with CO 2 and the initial rock temperature are further increased to 90 ℃, the rock temperature rise and the average CO 2 sealing rate are increased by more than 60% compared with those at 37 ℃, the rock temperature after 2 years is increased by 181 ℃, and the grade of the high-temperature geothermal grade is far more than 150 ℃. Meanwhile, the extraction efficiency of valuable elements nickel and cobalt exceeds 50%, the total CO 2 sealing benefit, geothermal benefit and valuable element mining and smelting benefit are obtained, and each sealing 1 ton of CO 2 can obtain remarkable economic benefit, so that the high cost situation of CO 2 geological sealing is thoroughly twisted. \|[0020] 2. The method provided by the invention is characterized in that under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade.\|DRAWINGS DESCRIPTION\|Description of the drawings:\|[0021] FIG. 1 is a schematic view of a geological vertical section of the invention with ammonium bisulfate assisted permanent sequestration of CO 2 while producing geothermal heat and extracting valuable elements. \|[0022] Fig. 2 is an X-ray diffraction spectrum of the sample of olivine of example 1.\|[0023] FIG. 3 is an electron microscopy image (a) and elemental scan spectra (b-d) of the olivine flakes of example 1.\|[0024] FIG. 4 is a plot of response surface and contour of the two-factor interaction versus magnesium response rate in example 2.\|[0025] FIG. 5 is a graph showing the surface reaction rate of the olivine with NH 4HSO4 as a function of (a) NH 4HSO4 and (b) 1/T in example 3.\|[0026] FIG. 6 is a graph of the K-penetration (c) after the treatment of the olivine, showing the results (a) of the K-penetration test before the treatment of the olivine, and the electron microscopic crack graph (b) of example 4.\|[0027] FIG. 7 is a simulation result after 2 years for different injection fluid temperatures and initial olivine temperatures in example 5, showing the results of geology indirect carbonization (Indirect) and geology Direct carbonization (Direct), respectively, wherein (a) is the average olivine temperature rise (in units:. Degree.C.); (b) The average CO 2 sequestration rate (unit: kg/(year. M 3)).\|[0028] Fig. 8 is a graph showing the effect of extracting nickel and cobalt as valuable elements in example 6.\|INVENTION MODE\|The specific embodiment is as follows:\|[0029] The following examples are further illustrative of the invention and are not intended to be limiting thereof. \|[0030] Unless defined otherwise, all technical and scientific terms used hereinafter have the same meaning as commonly understood by one of ordinary skill in the art. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the scope of the present invention. Unless otherwise indicated, the experimental materials and reagents herein are all commercially available products conventional in the art.\|[0031] As shown in fig. 1, a method for permanently sequestering carbon dioxide and simultaneously generating geothermal heat and extracting valuable elements by using geological rock assisted by ammonium bisulfate mainly relates to conventional geological drilling operation, pressurized injection of mixed fluid of CO 2 and ammonium bisulfate, drilling sealing, opening the drilling sealing after reaction is mature, and collecting steam and nickel-cobalt solution. The method specifically comprises the following steps:\|[0032] (1) Selecting injection and screening formation conditions: different injection conditions and stratum conditions bring different geological mineral carbonization effects, corresponding injection conditions are selected in different stratum conditions to improve the energy utilization rate, and the stratum conditions comprise: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, the stratum mineral volume is 1-1 multiplied by 10 20m3, and the injection conditions of the mixed fluid of carbon dioxide and ammonium bisulfate comprise: the liquid temperature is 20-200 ℃, the carbon dioxide pressure is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection; \|[0033] (2) Under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade. \|[0034] Example 1\|[0035] The analysis results of the components of the olivine adopted by the invention are shown in table 1, the NH 4HSO4 amount required for implementation is calculated according to the magnesium, calcium and iron contents, the theoretical carbonation capacity of the olivine mineral is calculated according to the total content of the magnesium, calcium and iron contents in the olivine, and the extractable nickel and cobalt amounts in each ton of olivine are respectively 3.31kg and 0.185kg. Figure 2 shows the X-ray diffraction spectrum of olivine showing that the main mineral composition in the rock sample is olivine Mg 2SiO4, accompanied by small amounts of chrysotile Mg 3Si2O5(OH)4, talc Mg 3Si4O10(OH)2 and iron oxide Fe 2O3. Fig. 3 shows the electron microscope and main element scan results of the olivine, showing the elemental distribution of magnesium, oxygen, silicon, respectively, on the rock surface, demonstrating that magnesium is primarily present in the silicate in the rock.\|[0036] TABLE 1 analysis of elements of olivine samples based on X-ray fluorescence spectra\|[0037] Element/OxideSiO2MgOFe2O3Al2O3CaOCr2O3NiOCoCuOTiO2wt%43.4837.248.570.700.500.470.330.020.010.01\|[0038] Example 2\|[0039] According to the center combination experimental design principle of Box-Benhnken, three factors which have obvious and common influence on magnesium reaction rate are selected, a three-factor three-level response surface analysis method is adopted on the basis of a single-factor experiment, and the experimental factors and the level design are shown in Table 2. FIG. 4 presents a response surface and contour plot of two-factor interaction versus magnesium response rate, which shows a significant logarithmic relationship between magnesium response rate and overall independent variables. The contour diagram shows that the extreme value exists under the conditions that the concentration of NH 4HSO4 is 1.62mol/L, the reaction temperature is 144 ℃ and the solid-liquid ratio is 30g/L, the theoretical magnesium reaction rate can reach 100%, the olivine magnesium extraction experiment is carried out by adopting the experimental conditions, the actual extraction rate is 95%, the relative error is about 5%, and the condition parameters obtained by the response surface analysis method are proved to be accurate and reliable. Comparing the three groups of graphs shows that the solid-liquid ratio has the most obvious effect on the magnesium extraction rate, the concentration of NH 4HSO4 is inferior, and the difference effect of the reaction temperature on the result is smaller.\|[0040] TABLE 2 response surface analysis factors and levels\|[0041] \|[0042] Example 3\|[0043] The NH 4HSO4 concentration and the experimental temperature were varied, and after 15s the solution was extracted and the magnesium content was measured to calculate the reaction rate, and the reaction conditions are shown in Table 3. FIG. 5 shows the trend of the surface reaction rate of olivine with NH 4HSO4 over NH 4HSO4 and 1/T, showing that the surface reaction rate of acid rock increases logarithmically with increasing concentration of NH 4HSO4 and exponentially with increasing temperature, we obtain a reaction progression of 0.462, a reaction activation energy of 36598J/mol, and a frequency factor of 0.184 using the fit equation and Arrhenius equation. Kinetic rate equation for extracting Mg by NH 4HSO4 reacting with the surface of olivine:\|[0044] \|[0045] Wherein J is the surface reaction rate (unit: mol/(cm 2. Multidot. S)), T is the reaction temperature (unit: DEG C), and C NH4HSO4 is the NH 4HSO4 concentration (unit: mol/L). \|[0046] TABLE 3 acid rock surface reaction conditions\|[0047] \|[0048] Example 4\|[0049] Taking the CO 2 phase-change jet fracturing method as an example, the permeability test and SEM test of CO 2 gas measurement before and after treatment are performed on the olivine core sample, and the permeability test results and SEM crack diagrams of the cores before and after treatment are shown in fig. 6. Experimental results showed that the permeability of the untreated sample was 0.1472uD (1 uD = 1 x 10 -3um2); after applying an overburden pressure of 12Mpa (equivalent to a geostatic pressure of about 500m depth) and heating to 40 ℃, the permeability was increased to 0.3862uD by CO 2 jet treatment at 14Mpa pressure, 2.62 times higher than the untreated sample. SEM test results show that the pore structure of the core slice is obviously changed before and after treatment, the crack depth is obviously deepened, and the number of cracks is obviously increased. Experiments prove that the CO 2 phase-change jet fracturing method can improve the permeability of rock.\|[0050] Example 5\|[0051] The average temperature of the stratum at 1000m is set to be 37 ℃, because the optimal temperature of geological direct carbonization is 185 ℃ and the middle point temperature is 90 ℃, 10 days are required for waiting for reaction maturation time after injection at the mixed fluid temperature of 150 ℃ and the carbon dioxide pressure of 20MPa, the concentration of NH 4HSO4 in the mixed fluid is 0.5mol/L, and the solid-to-liquid ratio of the solution of the olivine and NH 4HSO4 is 200kg/L. Figure 7 details the average olivine temperature rise and average CO 2 sequestration rate change after 2 years of geologically indirect carbonization and geologically direct carbonization. The calculation results show that the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization both tend to rise and then fall under the condition of considering heat dissipation, probably because the NH 4HSO4 endothermic decomposition temperature limits the area temperature rise. The average temperature rise of the olivine and the average CO 2 sequestration rate extreme value of the geology indirect carbonization are found at t0=90 ℃, tin=185 ℃, and are respectively 181 ℃ and 195 kg/(year-m 3), the average temperature of the olivine and the annual carbon sequestration quantity respectively reach 271 ℃ and 19.5 ten thousand tons, and the average temperature rise of the olivine and the annual carbon sequestration rate extreme value are improved by more than 60% compared with the lowest case (t0=37 ℃, tin=37 ℃). When T0 is the same, the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization are both in an ascending trend along with the increase of Tin. Compared with two mineral carbonization modes, when T0 and Tin are at lower temperature, the average olivine temperature rise and the average CO 2 sealing rate of the geology indirect carbonization are far greater than those of the geology indirect carbonization; when T0 and Tin are at higher temperatures, the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization are both higher than those of the geology direct carbonization, but the gap is reduced, and only when the T0 temperature is lower and the Tin temperature is higher, the average olivine temperature rise of the geology direct carbonization can exceed that of the geology indirect carbonization. This introduces a feature of geological indirect carbonization.\|[0052] As can be seen from fig. 7, the result of geologically indirect carbonization is less sensitive to temperature than geologically direct carbonization, which suggests that it has the potential to be applied to shallow olivine, since shallow olivine formations typically have lower initial temperatures. Taking the case of t0=37 ℃ and tin=37 ℃ which are easy to reach underground and ground as an example, the annual carbon sequestration amount can reach 19.5 ten thousand tons, approaching the optimal effect of geological direct carbonization in computation, the temperature of the olive strata can rise to 142 ℃ after 2 years, approaching the high-temperature geothermal grade, the stratum temperature level is only common in dry hot rocks deep in the earth at present, the depth is generally more than 3000m, and high drilling cost and fluid compression power consumption are required for developing the resource.\|[0053] Example 6\|[0054] Under the sealing conditions of example 5, other conditions are unchanged, ammonium bisulfate is replaced by HCl, HF, NH 4 Cl or NH 4HCO3, the extraction effect on high-value cobalt nickel element is compared, namely NH 4HSO4、HCl、HF、NH4 Cl or NH 4HCO3 is recovered, and the extraction efficiency of cobalt nickel element is detected, as shown in figure 8.\|[0055] As shown in Table 8, the extraction effect of NH 4SO4 and HCl on cobalt and nickel elements is equivalent, and because HCl is strong acid and is harmful to the environment, pollution is caused to water and soil, and the extraction efficiency of valuable elements nickel and cobalt is up to 90 percent by using ammonium bisulfate to assist in utilizing geological rock to seal carbon dioxide.\|[0056] Example 7\|[0057] An ammonium bisulfate assisted method for permanently sequestering carbon dioxide by using geological rock while generating geothermal heat and extracting valuable elements comprises the following steps: selecting injection and screening formation conditions: the formation conditions include: the injection conditions of the mixed fluid of the carbon dioxide and the ammonium bisulfate comprise that the underground depth is 0m, the surface temperature is 20 ℃, the formation flow pressure is 0.1MPa, the formation porosity is 50%, the formation permeability is 1 multiplied by 10 -2m2, the formation mineral volume is 1 to 1 multiplied by 10 20m3: the temperature of the mixed fluid is 20 ℃, the pressure of carbon dioxide is 0.1MPa, and the reaction maturation time is waited for 12 hours after injection; under the assistance of ammonium bisulfate, the mixed fluid of ammonium bisulfate and carbon dioxide is injected to react with the olivine through seepage and mass transfer to quickly generate stable carbonate, and meanwhile, high-value elements of nickel and cobalt rich in magnesium, calcium and iron silicate of the leaching solution are recovered.\|[0058] Example 8\|[0059] An ammonium bisulfate assisted method for permanently sequestering carbon dioxide by using geological rock while generating geothermal heat and extracting valuable elements comprises the following steps: selecting injection and screening formation conditions: the formation conditions include: the injection conditions of the mixed fluid of the carbon dioxide and the ammonium bisulfate comprise: the temperature of the mixed fluid is 200 ℃, the pressure of carbon dioxide is 40MPa, and the reaction maturation time is 3650 days after injection; under the assistance of ammonium bisulfate, the mixed fluid of ammonium bisulfate and carbon dioxide is injected to react with the olivine through seepage and mass transfer to quickly generate stable carbonate, and meanwhile, high-value elements of nickel and cobalt rich in magnesium, calcium and iron silicate of the leaching solution are recovered.\|[0060] The above embodiments are only described to assist in understanding the technical solution of the present invention and its core idea, and it should be noted that it will be obvious to those skilled in the art that several improvements and modifications can be made to the present invention without departing from the principle of the present invention, and these improvements and modifications also fall within the protection scope of the claims of the present invention.	(CN118189424)\|TECHNICAL FIELD\|[0001] The invention relates to the technical field of carbon dioxide sequestration, in particular to a method for generating geothermal heat and extracting valuable elements by permanently sequestering carbon dioxide by using geological rock with the aid of ammonium bisulfate. \|BACKGROUND ART\|The background technology is as follows:\|[0002] large scale carbon capture, utilization and sequestration (CCUS) technologies must be developed to achieve carbon neutralization, which involves injection of CO 2 into geological structures, such as deep brine layers or Enhanced Oil Recovery (EOR) in oil fields, but may involve leakage of freely stored CO 2 back to the atmosphere. \|[0003] The invention applied by the inventor realizes permanent fixation by utilizing the reaction of silicate minerals rich in magnesium, calcium and iron in geological strata and CO 2, but the risk of leakage of CO 2 back to the atmosphere can be greatly reduced and heat release is also accompanied; however, this process is very slow, and it is difficult and long time to accumulate valuable heat energy for use under the heat dissipation conditions of the geological structure, and the geological sequestration depth of CO 2 is generally better in the range of 2000-3000 meters, and this depth brings about thresholds such as drilling cost, compression energy consumption of CO 2, and the like.\|[0004] In view of the fact that geothermal energy has become one of the most competitive renewable energy utilization modes, the CO 2 geological sequestration is indeed capable of generating geothermal-like heat for utilization, and a new method is needed to achieve carbon dioxide sequestration while improving geothermal grade.\|DISCLOSURE\|The invention comprises the following steps:\|[0005] Aiming at the problems existing in the prior art, the invention provides a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide assisted by ammonium bisulfate, which can obviously accelerate the carbonization reaction path of minerals in stratum, accelerate heat release by faster reaction, drive considerable temperature rise of the rock and improve geothermal grade and economic benefit feasibility of heat collection. \|[0006] The invention aims to provide a method for generating geothermal heat and extracting valuable elements by using geological rock to permanently seal carbon dioxide in an auxiliary manner by ammonium bisulfate, which comprises the following steps of: under the assistance of ammonium bisulfate, silicate minerals containing magnesium, calcium and iron in a geological structure react with injected carbon dioxide, permanently seal the carbon dioxide, simultaneously generate geothermal heat and recover valuable elements rich in silicate in leaching liquid.\|[0007] The invention discloses a carbonization reaction path capable of remarkably accelerating minerals in a stratum, accelerating heat release by faster reaction, driving considerable temperature rise of rock, and improving geothermal grade and economic benefit feasibility of heat collection. According to the invention, strong acid weak alkali salt (ammonium bisulfate NH 4HSO4) is adopted to accelerate the reaction of magnesium calcium silicate in a geological structure and injected CO 2, NH 4HSO4 has the potential of recycling, nickel and cobalt high-value elements rich in magnesium, calcium and iron silicate in leaching liquid are recovered, the nickel and cobalt productivity is improved to meet the requirements of clean energy sources of electric automobiles, the carbon footprint in mining activities is reduced, and high-purity amorphous silicon dioxide and brucite produced by subsequent processing of the solution can also be used for other chemical production.\|[0008] The method provided by the invention is characterized in that under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade.\|[0009] Preferably, the method specifically comprises the following steps: injecting a mixed fluid of ammonium bisulfate and carbon dioxide into a stratum of silicate minerals containing magnesium, calcium and iron, reacting the mixed fluid with the silicate minerals containing magnesium, calcium and iron to generate carbonate, permanently sealing carbon dioxide, simultaneously coupling heat release and reaction rate to improve geothermal grade, and recovering valuable elements nickel and cobalt rich in silicate in the leaching solution.\|[0010] The method provided by the invention is to inject the mixed fluid of CO 2 and ammonium bisulfate into a well, seal the well, open the well after the reaction is mature, collect steam and nickel-cobalt solution, realize that geological rock permanently seals carbon dioxide to generate geothermal heat and extract valuable elements nickel-cobalt.\|[0011] The invention continuously pushes the proposed silicate minerals which are rich in magnesium, calcium and iron in geological strata to react with CO 2 to realize permanent fixation technology, adopts strong acid weak alkali salt (such as ammonium bisulfate NH 4HSO4), accelerates the reaction of magnesium calcium silicate rock in geological structures with injected CO 2, and NH 4HSO4 has recoverable recycling potential, simultaneously recovers nickel and cobalt high-value elements which are rich in magnesium, calcium and iron silicate in leaching solution, improves the nickel and cobalt capacity to meet the requirements of clean energy of electric vehicles, reduces the carbon footprint in mining activities, ensures that the high-purity amorphous silicon dioxide and brucite which are produced by subsequent processing of the solution can also be used for other chemical production, changes the defect of very slow conventional permanent sealing reaction rate, improves the sealing geological grade, simultaneously reduces the sealing geological depth, and obtains high-value elements including recovered nickel and cobalt, reduces the cost, the compression energy consumption of CO 2 and the like.\|[0012] Preferably, the formation conditions include: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3. Different injection conditions and stratum conditions bring different geological mineral carbonization effects, and corresponding injection conditions are selected under different stratum conditions, so that the energy utilization rate is improved. Further preferably, the formation conditions include: the underground depth is 1000-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, and the stratum mineral volume is 1-1 multiplied by 10 20m3.\|[0013] Preferably, the injection conditions of the mixed fluid of ammonium bisulfate and carbon dioxide comprise: the temperature of the mixed fluid is 20-200 ℃, the pressure of carbon dioxide is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection.\|[0014] Preferably, the geothermal grade is a medium and high temperature geothermal grade greater than 150 ℃.\|[0015] Preferably, the silicate minerals include olivine, serpentine, basalt, wollastonite and anorthite which are rich in magnesium, calcium and iron.\|[0016] Preferably, the concentration of NH 4HSO4 in the mixed fluid is 0.1-2.0mol/L, the solid-to-liquid ratio of silicate mineral to NH 4HSO4 solution is 100-1000kg/L, and the reaction temperature is 50-180 ℃.\|[0017] The invention also protects the application of the method in carbon dioxide sequestration.\|[0018] Compared with the prior art, the invention has the following advantages:\|[0019] 1. According to the method provided by the invention, in the geological rock and 2-year period, the initial temperature of the related geological rock stratum and the temperature of the CO 2 fluid injected are 37 ℃ and 1 cubic kilometer, the average temperature rise of the rock can reach 105 ℃ and reach 142 ℃ at the final temperature, high geothermal grade reaction heat is generated, and meanwhile, the geological storage CO 2 amount can reach 11.9 ten thousand tons each year, which is equivalent to the annual carbon storage amount of 342k square kilometer forests in northwest China; if the temperature of the fluid injected with CO 2 and the initial rock temperature are further increased to 90 ℃, the rock temperature rise and the average CO 2 sealing rate are increased by more than 60% compared with those at 37 ℃, the rock temperature after 2 years is increased by 181 ℃, and the grade of the high-temperature geothermal grade is far more than 150 ℃. Meanwhile, the extraction efficiency of valuable elements nickel and cobalt exceeds 50%, the total CO 2 sealing benefit, geothermal benefit and valuable element mining and smelting benefit are obtained, and each sealing 1 ton of CO 2 can obtain remarkable economic benefit, so that the high cost situation of CO 2 geological sealing is thoroughly twisted. \|[0020] 2. The method provided by the invention is characterized in that under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade.\|DRAWINGS DESCRIPTION\|Description of the drawings:\|[0021] FIG. 1 is a schematic view of a geological vertical section of the invention with ammonium bisulfate assisted permanent sequestration of CO 2 while producing geothermal heat and extracting valuable elements. \|[0022] Fig. 2 is an X-ray diffraction spectrum of the sample of olivine of example 1.\|[0023] FIG. 3 is an electron microscopy image (a) and elemental scan spectra (b-d) of the olivine flakes of example 1.\|[0024] FIG. 4 is a plot of response surface and contour of the two-factor interaction versus magnesium response rate in example 2.\|[0025] FIG. 5 is a graph showing the surface reaction rate of the olivine with NH 4HSO4 as a function of (a) NH 4HSO4 and (b) 1/T in example 3.\|[0026] FIG. 6 is a graph of the K-penetration (c) after the treatment of the olivine, showing the results (a) of the K-penetration test before the treatment of the olivine, and the electron microscopic crack graph (b) of example 4.\|[0027] FIG. 7 is a simulation result after 2 years for different injection fluid temperatures and initial olivine temperatures in example 5, showing the results of geology indirect carbonization (Indirect) and geology Direct carbonization (Direct), respectively, wherein (a) is the average olivine temperature rise (in units:. Degree.C.); (b) The average CO 2 sequestration rate (unit: kg/(year. M 3)).\|[0028] Fig. 8 is a graph showing the effect of extracting nickel and cobalt as valuable elements in example 6.\|INVENTION MODE\|The specific embodiment is as follows:\|[0029] The following examples are further illustrative of the invention and are not intended to be limiting thereof. \|[0030] Unless defined otherwise, all technical and scientific terms used hereinafter have the same meaning as commonly understood by one of ordinary skill in the art. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the scope of the present invention. Unless otherwise indicated, the experimental materials and reagents herein are all commercially available products conventional in the art.\|[0031] As shown in fig. 1, a method for permanently sequestering carbon dioxide and simultaneously generating geothermal heat and extracting valuable elements by using geological rock assisted by ammonium bisulfate mainly relates to conventional geological drilling operation, pressurized injection of mixed fluid of CO 2 and ammonium bisulfate, drilling sealing, opening the drilling sealing after reaction is mature, and collecting steam and nickel-cobalt solution. The method specifically comprises the following steps:\|[0032] (1) Selecting injection and screening formation conditions: different injection conditions and stratum conditions bring different geological mineral carbonization effects, corresponding injection conditions are selected in different stratum conditions to improve the energy utilization rate, and the stratum conditions comprise: the underground depth is 0-5000 m, the stratum temperature is 20-200 ℃, the stratum flow pressure is 0.1-30MPa, the stratum porosity is 0.01-50%, the stratum permeability is 1 multiplied by 10 -20-1 x 10-10m2, the stratum mineral volume is 1-1 multiplied by 10 20m3, and the injection conditions of the mixed fluid of carbon dioxide and ammonium bisulfate comprise: the liquid temperature is 20-200 ℃, the carbon dioxide pressure is 0.1-40MPa, and the reaction maturation time is 0.5-3650 days after injection; \|[0033] (2) Under the assistance of ammonium bisulfate, the injected carbon dioxide mixed solution reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is quickly generated, the mineralization fixing process is faster, meanwhile, the heat release and the reaction rate are coupled to promote the geothermal grade, the ammonium bisulfate accelerates the reaction to cause the mineralization reaction rate, and the heat release process of the mineral carbonization reaction is coupled with the reaction rate to promote the geothermal grade. \|[0034] Example 1\|[0035] The analysis results of the components of the olivine adopted by the invention are shown in table 1, the NH 4HSO4 amount required for implementation is calculated according to the magnesium, calcium and iron contents, the theoretical carbonation capacity of the olivine mineral is calculated according to the total content of the magnesium, calcium and iron contents in the olivine, and the extractable nickel and cobalt amounts in each ton of olivine are respectively 3.31kg and 0.185kg. Figure 2 shows the X-ray diffraction spectrum of olivine showing that the main mineral composition in the rock sample is olivine Mg 2SiO4, accompanied by small amounts of chrysotile Mg 3Si2O5(OH)4, talc Mg 3Si4O10(OH)2 and iron oxide Fe 2O3. Fig. 3 shows the electron microscope and main element scan results of the olivine, showing the elemental distribution of magnesium, oxygen, silicon, respectively, on the rock surface, demonstrating that magnesium is primarily present in the silicate in the rock.\|[0036] TABLE 1 analysis of elements of olivine samples based on X-ray fluorescence spectra\|[0037] Element/OxideSiO2MgOFe2O3Al2O3CaOCr2O3NiOCoCuOTiO2wt%43.4837.248.570.700.500.470.330.020.010.01\|[0038] Example 2\|[0039] According to the center combination experimental design principle of Box-Benhnken, three factors which have obvious and common influence on magnesium reaction rate are selected, a three-factor three-level response surface analysis method is adopted on the basis of a single-factor experiment, and the experimental factors and the level design are shown in Table 2. FIG. 4 presents a response surface and contour plot of two-factor interaction versus magnesium response rate, which shows a significant logarithmic relationship between magnesium response rate and overall independent variables. The contour diagram shows that the extreme value exists under the conditions that the concentration of NH 4HSO4 is 1.62mol/L, the reaction temperature is 144 ℃ and the solid-liquid ratio is 30g/L, the theoretical magnesium reaction rate can reach 100%, the olivine magnesium extraction experiment is carried out by adopting the experimental conditions, the actual extraction rate is 95%, the relative error is about 5%, and the condition parameters obtained by the response surface analysis method are proved to be accurate and reliable. Comparing the three groups of graphs shows that the solid-liquid ratio has the most obvious effect on the magnesium extraction rate, the concentration of NH 4HSO4 is inferior, and the difference effect of the reaction temperature on the result is smaller.\|[0040] TABLE 2 response surface analysis factors and levels\|[0041] \|[0042] Example 3\|[0043] The NH 4HSO4 concentration and the experimental temperature were varied, and after 15s the solution was extracted and the magnesium content was measured to calculate the reaction rate, and the reaction conditions are shown in Table 3. FIG. 5 shows the trend of the surface reaction rate of olivine with NH 4HSO4 over NH 4HSO4 and 1/T, showing that the surface reaction rate of acid rock increases logarithmically with increasing concentration of NH 4HSO4 and exponentially with increasing temperature, we obtain a reaction progression of 0.462, a reaction activation energy of 36598J/mol, and a frequency factor of 0.184 using the fit equation and Arrhenius equation. Kinetic rate equation for extracting Mg by NH 4HSO4 reacting with the surface of olivine:\|[0044] \|[0045] Wherein J is the surface reaction rate (unit: mol/(cm 2. Multidot. S)), T is the reaction temperature (unit: DEG C), and C NH4HSO4 is the NH 4HSO4 concentration (unit: mol/L). \|[0046] TABLE 3 acid rock surface reaction conditions\|[0047] \|[0048] Example 4\|[0049] Taking the CO 2 phase-change jet fracturing method as an example, the permeability test and SEM test of CO 2 gas measurement before and after treatment are performed on the olivine core sample, and the permeability test results and SEM crack diagrams of the cores before and after treatment are shown in fig. 6. Experimental results showed that the permeability of the untreated sample was 0.1472uD (1 uD = 1 x 10 -3um2); after applying an overburden pressure of 12Mpa (equivalent to a geostatic pressure of about 500m depth) and heating to 40 ℃, the permeability was increased to 0.3862uD by CO 2 jet treatment at 14Mpa pressure, 2.62 times higher than the untreated sample. SEM test results show that the pore structure of the core slice is obviously changed before and after treatment, the crack depth is obviously deepened, and the number of cracks is obviously increased. Experiments prove that the CO 2 phase-change jet fracturing method can improve the permeability of rock.\|[0050] Example 5\|[0051] The average temperature of the stratum at 1000m is set to be 37 ℃, because the optimal temperature of geological direct carbonization is 185 ℃ and the middle point temperature is 90 ℃, 10 days are required for waiting for reaction maturation time after injection at the mixed fluid temperature of 150 ℃ and the carbon dioxide pressure of 20MPa, the concentration of NH 4HSO4 in the mixed fluid is 0.5mol/L, and the solid-to-liquid ratio of the solution of the olivine and NH 4HSO4 is 200kg/L. Figure 7 details the average olivine temperature rise and average CO 2 sequestration rate change after 2 years of geologically indirect carbonization and geologically direct carbonization. The calculation results show that the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization both tend to rise and then fall under the condition of considering heat dissipation, probably because the NH 4HSO4 endothermic decomposition temperature limits the area temperature rise. The average temperature rise of the olivine and the average CO 2 sequestration rate extreme value of the geology indirect carbonization are found at t0=90 ℃, tin=185 ℃, and are respectively 181 ℃ and 195 kg/(year-m 3), the average temperature of the olivine and the annual carbon sequestration quantity respectively reach 271 ℃ and 19.5 ten thousand tons, and the average temperature rise of the olivine and the annual carbon sequestration rate extreme value are improved by more than 60% compared with the lowest case (t0=37 ℃, tin=37 ℃). When T0 is the same, the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization are both in an ascending trend along with the increase of Tin. Compared with two mineral carbonization modes, when T0 and Tin are at lower temperature, the average olivine temperature rise and the average CO 2 sealing rate of the geology indirect carbonization are far greater than those of the geology indirect carbonization; when T0 and Tin are at higher temperatures, the average olivine temperature rise and the average CO 2 sequestration rate of the geology indirect carbonization are both higher than those of the geology direct carbonization, but the gap is reduced, and only when the T0 temperature is lower and the Tin temperature is higher, the average olivine temperature rise of the geology direct carbonization can exceed that of the geology indirect carbonization. This introduces a feature of geological indirect carbonization.\|[0052] As can be seen from fig. 7, the result of geologically indirect carbonization is less sensitive to temperature than geologically direct carbonization, which suggests that it has the potential to be applied to shallow olivine, since shallow olivine formations typically have lower initial temperatures. Taking the case of t0=37 ℃ and tin=37 ℃ which are easy to reach underground and ground as an example, the annual carbon sequestration amount can reach 19.5 ten thousand tons, approaching the optimal effect of geological direct carbonization in computation, the temperature of the olive strata can rise to 142 ℃ after 2 years, approaching the high-temperature geothermal grade, the stratum temperature level is only common in dry hot rocks deep in the earth at present, the depth is generally more than 3000m, and high drilling cost and fluid compression power consumption are required for developing the resource.\|[0053] Example 6\|[0054] Under the sealing conditions of example 5, other conditions are unchanged, ammonium bisulfate is replaced by HCl, HF, NH 4 Cl or NH 4HCO3, the extraction effect on high-value cobalt nickel element is compared, namely NH 4HSO4、HCl、HF、NH4 Cl or NH 4HCO3 is recovered, and the extraction efficiency of cobalt nickel element is detected, as shown in figure 8.\|[0055] As shown in Table 8, the extraction effect of NH 4SO4 and HCl on cobalt and nickel elements is equivalent, and because HCl is strong acid and is harmful to the environment, pollution is caused to water and soil, and the extraction efficiency of valuable elements nickel and cobalt is up to 90 percent by using ammonium bisulfate to assist in utilizing geological rock to seal carbon dioxide.\|[0056] Example 7\|[0057] An ammonium bisulfate assisted method for permanently sequestering carbon dioxide by using geological rock while generating geothermal heat and extracting valuable elements comprises the following steps: selecting injection and screening formation conditions: the formation conditions include: the injection conditions of the mixed fluid of the carbon dioxide and the ammonium bisulfate comprise that the underground depth is 0m, the surface temperature is 20 ℃, the formation flow pressure is 0.1MPa, the formation porosity is 50%, the formation permeability is 1 multiplied by 10 -2m2, the formation mineral volume is 1 to 1 multiplied by 10 20m3: the temperature of the mixed fluid is 20 ℃, the pressure of carbon dioxide is 0.1MPa, and the reaction maturation time is waited for 12 hours after injection; under the assistance of ammonium bisulfate, the mixed fluid of ammonium bisulfate and carbon dioxide is injected to react with the olivine through seepage and mass transfer to quickly generate stable carbonate, and meanwhile, high-value elements of nickel and cobalt rich in magnesium, calcium and iron silicate of the leaching solution are recovered.\|[0058] Example 8\|[0059] An ammonium bisulfate assisted method for permanently sequestering carbon dioxide by using geological rock while generating geothermal heat and extracting valuable elements comprises the following steps: selecting injection and screening formation conditions: the formation conditions include: the injection conditions of the mixed fluid of the carbon dioxide and the ammonium bisulfate comprise: the temperature of the mixed fluid is 200 ℃, the pressure of carbon dioxide is 40MPa, and the reaction maturation time is 3650 days after injection; under the assistance of ammonium bisulfate, the mixed fluid of ammonium bisulfate and carbon dioxide is injected to react with the olivine through seepage and mass transfer to quickly generate stable carbonate, and meanwhile, high-value elements of nickel and cobalt rich in magnesium, calcium and iron silicate of the leaching solution are recovered.\|[0060] The above embodiments are only described to assist in understanding the technical solution of the present invention and its core idea, and it should be noted that it will be obvious to those skilled in the art that several improvements and modifications can be made to the present invention without departing from the principle of the present invention, and these improvements and modifications also fall within the protection scope of the claims of the present invention.	Family Number\|(110191082)\|110191082\|Object of Invention\|(CN118189424 A)\|The invention relates to the technical field of carbon dioxide sequestration , in particular to a method for generating geothermal heat and extracting valuable elements by permanently sequestering carbon dioxide by using geological rock with the aid of ammonium bisulfate . \|Abstract\|(CN118189424 A)\|The invention discloses a method for generating terrestrial heat and extracting valuable elements by permanently sealing and storing carbon dioxide through geological rocks under the assistance of ammonium bisulfate . The method comprises the following steps that under the assistance of ammonium bisulfate , silicate rock minerals containing magnesium , calcium and iron in a geologic structure react with injected carbon dioxide , carbon dioxide is permanently sealed , meanwhile , terrestrial heat is generated , and valuable elements rich in leachate silicate are recycled . According to the method , under the assistance of ammonium bisulfate , injected carbon dioxide mixed liquid reacts with silicate geological minerals containing magnesium , calcium and iron through seepage and mass transfer , stable carbonate is rapidly generated , the mineralization fixing process is fast , meanwhile , heat release and the reaction rate are coupled to improve the geothermal grade , the reaction is accelerated through ammonium bisulfate , the mineralization reaction rate is increased , and the mineralization effect is improved . The heat release process of the mineral carbonization reaction is coupled with the reaction rate to improve the geothermal grade . \|	Materials, metallurgy\|Thermal processes and apparatus	C01B-033/12/6\|C01F-005/14\|C01G-051/00\|C01G-053/00\|C01P-2006/80\|C22B-003/04\|C22B-023/0415\|F24T-010/00\|F24V-030/00\|F28D-020/00/52		C01B-033/12/6\|C01F-005/14\|C01G-051/00\|C01G-053/00\|C01P-2006/80\|C22B-003/04\|C22B-023/0415\|F24T-010/00\|F24V-030/00\|F28D-020/00/52	C01B-033/12\|C01F-005/14\|C01G-051/00\|C01G-053/00\|C22B-003/04\|C22B-023/00\|F24T-010/00\|F24V-030/00\|F28D-020/00	C01B-033/12\|C01F-005/14\|C01G-051/00\|C01G-053/00\|C22B-003/04\|C22B-023/00\|F24T-010/00\|F24V-030/00\|F28D-020/00			CN118423599	CN118423599 110862844 WHO=Examiner SELF=N CAT=A						PENDING	(CN118189424)\|PENDING	ALIVE	(CN118189424)\|ALIVE	(CN118189424)\|LEGAL DETAILS FOR CN118189424\|Actual or expected expiration date=2044-03-15\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-03-15\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202410297703\|Application date=2024-03-15\|Standardized application number=2024CN-0297703\|Event publication date=2024-06-14\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN118189424\|Publication stage code=A\|Publication date=2024-06-14\|Standardized publication number=CN118189424\|Event publication date=2024-06-14\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2024-07-02\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN118189424)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTO/ioLPE5/vlfn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000073203207&ekey=2149&xpn=CN118189424&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=PBZzTIHmhIfplFjK9nH8lZNXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN118189424)\|CN	(CN118189424)\|NAME=GUANGZHOU INSTITUTE OF ENERGY CONVERSION CHINESE ACADEMY OF SCIENCES , COUNTRY=CN		(CN118189424)\|NAME=FANG YAN;GUANGZHOU KEYUE I.P. LAW OFFICE , REG=44001NAME=MO YAOJIANG;GUANGZHOU KEYUE I.P. LAW OFFICE , REG=44001		(CN118189424)\|NAME=CAO YAN	(CN118189424)\|8	1	1					(CN118189424)\|Number of Claims: NCL=8\|Gazette date: GAZDATE=2024-06-14\|Gazette number: GAZNUM=40-2402\|Number of Pages: NPAGES=14\|		(CN118189424)\|CHINESE (CHI)	(CN118189424)\|Patent	Titre: (CN118189424)\|Method for generating terrestrial heat and extracting valuable elements by permanently sealing carbon dioxide through geological rock under assistance of ammonium bisulfate Résumé: (CN118189424)\|The invention discloses a method for generating terrestrial heat and extracting valuable elements by permanently sealing and storing carbon dioxide through geological rocks under the assistance of ammonium bisulfate. The method comprises the following steps that under the assistance of ammonium bisulfate, silicate rock minerals containing magnesium, calcium and iron in a geologic structure react with injected carbon dioxide, carbon dioxide is permanently sealed, meanwhile, terrestrial heat is generated, and valuable elements rich in leachate silicate are recycled. According to the method, under the assistance of ammonium bisulfate, injected carbon dioxide mixed liquid reacts with silicate geological minerals containing magnesium, calcium and iron through seepage and mass transfer, stable carbonate is rapidly generated, the mineralization fixing process is fast, meanwhile, heat release and the reaction rate are coupled to improve the geothermal grade, the reaction is accelerated through ammonium bisulfate, the mineralization reaction rate is increased, and the mineralization effect is improved. The heat release process of the mineral carbonization reaction is coupled with the reaction rate to improve the geothermal grade.	27	Abstract	gpt-4o-mini	yes	The method involves the reaction of silicate rock minerals with injected CO₂ to generate stable carbonates, which aligns with the goal of carbon sequestration and enhanced weathering.
32	SG2013095575\|WOSG2014/000613\|SG11201605164Y	WOSG2014/000613\|AU2014370454\|US15/107,870\|SG11201605164Y	AU2014370454\|US9896741\|US20160319395\|SG11201605164Y\|AU2014370454\|SG11201605164Y\|WO2015/099612	69805816	WO2015/099612 A1 2015-07-02 [WO201599612]\|AU2014370454 B2 2019-05-16 [AU2014370454]\|AU2014370454 A1 2016-07-28 [AU2014370454]\|US9896741 B2 2018-02-20 [US9896741]\|US20160319395 A1 2016-11-03 [US20160319395]\|SG11201605164Y B 2016-10-31 [SG11201605164Y]\|SG11201605164Y A 2016-07-28 [SG11201605164Y]	2013-12-24\|2014-12-23	2014-12-23\|2014-12-23\|2014-12-23\|2014-12-23	2019-05-16\|2018-02-20\|2016-11-03\|2016-10-31\|2016-07-28\|2016-07-28\|2015-07-02	(US9896741)\|2018-02-20\|\|(AU2014370454)\|2019-05-16\|(SG11201605164Y)\|2016-10-31	(US9896741)\|2035-01-20\|(WO2015/099612)\|2017-06-24\|(AU2014370454)\|2034-12-23\|(SG11201605164Y)\|2034-12-23	(US9896741)\|Method of producing metal carbonate from an ultramafic rock material	(US9896741)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.	A STAR - AGENCY FOR SCIENCE TECHNOLOGY & RESEARCH	(US9896741)\|Agency for Science, Technology and Research ([SG])\|(US20160319395)\|Agency for Science, Technology and Research ([SG])\|(WO2015/099612)\|AGENCY FOR SCIENCE, TECHNOLOGY AND RESEARCH ([SG])\|(AU2014370454)\|Agency for Science, Technology and Research\|(AU2014370454)\|Agency for Science, Technology and Research\|(SG11201605164Y)\|AGENCY FOR SCIENCE, TECHNOLOGY AND RESEARCH ([SG])\|(SG11201605164Y)\|AGENCY FOR SCIENCE, TECHNOLOGY AND RESEARCH ([SG])	BU JIE\|YEO TZE YUEN\|SHARRATT PAUL	(US9896741)\|Bu Jie\|Yeo Tze Yuen\|Sharratt Paul\|(US20160319395)\|Bu Jie\|Yeo Tze Yuen\|Sharratt Paul	(US9896741)\|Winstead, P.C.\|(WO2015/099612)\|VIERING, JENTSCHURA & PARTNER LLP ([SG])\|(AU2014370454)\|Phillips Ormonde Fitzpatrick ([AU])\|(SG11201605164Y)\|VIERING, JENTSCHURA & PARTNER LLP ([SG])\|Reg. Nb: T06LL1666B	(US9896741)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|Iron (III) oxide may be precipitated out from the mixture following oxidation to allow their easy removal.\|Thus, it is desirable to use concentrated solutions or gases in order to reduce infrastructure and operating costs.\|Since it is nearly impossible to inhibit the co-extraction of these elements during the acid leaching step, it is necessary to remove them in a separate step to separate Fe, Ni, Mn and Cr oxides, which are high value added metal salts, to ensure that high purity magnesite is obtained at the end of the process.\|	(US9896741)\|1. A method of producing a metal carbonate from an ultramafic rock material, the method comprising a) providing an ultramafic rock material comprising a metal silicate; b) reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; c) contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; d) heating the resultant mixture from step c) to decompose the salt of the metal to form metal oxide; and e) reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|16. A system for producing a metal carbonate from ultramafic rock material, the system comprising a) a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal; b) an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; c) a furnace configured to heat the resultant mixture from step b) to decompose the salt of the metal to form the metal oxide; and d) a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|	(US9896741)\|In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided.\|The invention relates to methods of producing metal carbonate from an ultramafic rock material.\|The method of the first aspect includes heating the resultant mixture following contact with oxygen to decompose the salt of the metal to form metal oxide.\|	(US9896741)\|ULTRAMAFIC ROCK MATERIAL(100,36)\|METAL CARBONATE(100,29)\|AERATE IMPURITY(100,9)\|METAL PRODUCTION(100,5)\|PRODUCING METAL CARBONATE(100,5)\|SALT DECOMPOSITION(89,8)\|PURITY MAGNESITE(73,1)\|ULTRAMAFIC ROCK(54,20)\|AQUEOUS CHESHUNT MIXTURE(54,17)\|PRECIPITATOR(46,8)\|ACID RESIDUE(43,10)\|COEXTRACTION(42,1)\|METHANEDIONE(38,22)\|CHESHUNT MIXTURE(36,20)\|CR OXIDE(36,1)\|METHANEDIONE REACTION(32,2)\|AIR STRIPPER COLUMN(30,19)\|METAL SILICATE(30,8)\|RECYCLING(28,4)\|FURNACE(27,10)\|REACTOR(27,6)\|SALT HYDRATION(27,5)\|ACIDIC VAPOR(26,4)\|INFRASTRUCTURE(25,3)\|AQUEOUS AMMONIA MOLAR RATIO(24,2)\|ACID LEACHING(24,1)\|METAL OXIDE(21,21)\|AMBIENT CONDITION(16,2)\|MAFIC MINERAL(15,3)\|MGCL2 6H2O HYDROLYSIS(14,1)\|GAS LIQUID PACKED COLUMN(13,7)\|ULTRAMAFIC ROCK PARTICLE(13,3)\|MGCL2 6H2O MOLE(13,1)\|PACKED SCRUBBING TOWER(13,1)\|HYDROHALIC ACID(12,3)\|CONCENTRATED SOLUTION(12,2)\|MGCL2 4H2O(12,2)\|CO2 EMISSION MITIGATION(11,1)\|NIO MNO PERCENT(11,1)\|CARBONATION REACTION(10,2)\|HEXAHYDRATE SALT(10,2)\|MAXIMAL DIMENSION(10,2)\|ACCELERATE LIBERATION(10,1)\|AQUEOUS AMMONIA FEASIBILITY(10,1)\|CHANGI WWTP(10,1)\|CO2 MINERALIZATION(10,1)\|DECOMPOSITION THERMODYNAMICS(10,1)\|GASEOUS METHANEDIONE(10,1)\|METAIGNEOUS ROCK(10,1)\|METHANEDIONE CAPTURE(10,1)\|NET CO2 CAPTURE(10,1)\|PACKING RESTRAINER(10,1)\|PASIR PANJANG(10,1)\|PULAU SAKRA(10,1)\|PULAU SERAYA(10,1)\|SINGAPORE OLEFIN(10,1)\|SMPO COGEN(10,1)\|SUBGENERIC GROUPING(10,1)\|VAPOR RECOMPRESSOR(10,1)\|MG3SI2O(8,4)\|ACID DIGESTION(8,2)\|AMPLE OPPORTUNITY(8,1)\|INDUSTRY INFRASTRUCTURE(8,1)\|LEACHING REQUIREMENT(8,1)\|MGCL2 2H2O(8,1)\|OPERATING COST(8,1)\|SERPENTINE ORE(8,1)\|SIMULTANEOUS EVAPORATION(8,1)\|STRATEGIC IMPORTANCE(8,1)\|MANGANESE(7,7)\|CHROMIUM(7,6)\|THERMOGRAVIMETRIC ANALYSIS(7,4)\|CO2 REMOVAL(7,3)\|COAL GASIFICATION(7,3)\|REEMISSION(7,3)\|AMMONIA CAPTURE(7,1)\|AQUEOUS LEACHING(7,1)\|CO2 CAPTURE REACTION(7,1)\|CO2 TON(7,1)\|CONCENTRATED LEACHATE SOLUTION(7,1)\|DIHYDRATE SALT(7,1)\|DIVERSE INDUSTRY(7,1)\|KEEPING ELECTRICITY(7,1)\|LEACHATE SOLUTION PH(7,1)\|LEACHATE STREAM(7,1)\|MG DECOMPOSITION(7,1)\|MGO MOL(7,1)\|MINERALIZATION REACTION(7,1)\|PURIFIED LEACHATE SOLUTION(7,1)\|SATURATED LEACHATE SOLUTION(7,1)\|SLOW DEHYDRATION(7,1)\|T CO2 HR TUA(7,1)\|TANK AGITATION(7,1)\|TETRAHYDRATE SALT(7,1)\|VALUE ADDED METAL SALT(7,1)\|HEATED AIR STRIPPER(6,5)\|11H2O(6,2)\|ALKALINE EARTH SILICATE MINERAL(6,2)\|EVAPORATOR(6,2)\|FIRE RETARDANT(6,2)\|HYDROGEN CHLORIDE STRIPPING(6,2)\|LAND RECLAMATION(6,2)\|METAL REFINERY(6,2)\|NEXT DECADE(6,2)\|NITROUS PRODUCT(6,2)\|HEAVY INDUSTRY(5,4)\|STEAM(5,4)\|HEATING MEDIUM(5,3)\|LEACHING(5,3)\|HSC(5,2)\|CARBONATION PRODUCT(5,1)\|COARSE SILICA SOLID RESIDUE(5,1)\|COMMERCIALIZATION(5,1)\|DESIGNED SCRUBBER(5,1)\|EFFLUENT TREATMENT(5,1)\|ELECTROLYTIC PRODUCTION(5,1)\|ESTABLISHED FUNDAMENTAL(5,1)\|GLOBAL METHANEDIONE LEVEL(5,1)\|GLOBAL SCALE(5,1)\|HARTSHORN(5,1)\|HYDRATED METAL SALT CRYSTALIZATION(5,1)\|INORGANIC SAMPLE(5,1)\|IRON OXIDATION(5,1)\|IRON SEPARATING OXIDE(5,1)\|LEACHING MEDIUM(5,1)\|LIQUID REDISTRIBUTOR(5,1)\|LISTED ITEM(5,1)\|METHANEDIONE GAS(5,1)\|NARROW SPECIES(5,1)\|NUMEROUS NITROGEN SPECIES(5,1)\|REGENERATION REACTION(5,1)\|REMOVING IMPURITY(5,1)\|SINGAPORE CHEMICAL(5,1)\|SOLID MGO RESIDUE(5,1)\|SOLUTION WARMING(5,1)\|TON CO2(5,1)\|UNCONTROLLED FORMATION(5,1)\|HYDROGEN CHLORIDE GAS(4,4)\|5H2O(4,1)\|AERATION(4,1)\|ANHYDROUS MAGNESIUM CHLORIDE(4,1)\|ASCENDING AIR(4,1)\|AUTOHYDROLYSIS DEGREE(4,1)\|AVERAGE SCALE(4,1)\|BLOWER(4,1)\|CLINOPYROXENE(4,1)\|CO2 LOSS(4,1)\|COMPARABLE SOLUTION(4,1)\|COMPLICATION FREE REGENERATION(4,1)\|CONSUMER(4,1)\|CONTAMINANT(4,1)\|CRUSHING(4,1)\|CRYSTALIZATION WATER(4,1)\|DEBACTEROL(4,1)\|DISSOLUTION HEAT(4,1)\|ELEMENT MGO(4,1)\|EXPERIMENT(4,1)\|FERRIC CHLORIDE CONVERSION(4,1)\|FILTRATE(4,1)\|GENUS(4,1)\|GIGATONNE(4,1)\|HEMATITE(4,1)\|HYDROGEN CHLORIDE REGENERATION(4,1)\|HYDROMAGNESITE(4,1)\|INSULATION(4,1)\|INTERMEDIATE SPECIES OXIDATION(4,1)\|IRON CONTENT(4,1)\|JURONG(4,1)\|KINETICS(4,1)\|LEACHING RATE(4,1)\|METAL CHLORIDE HYDROLYSIS(4,1)\|METAL LIBERATION(4,1)\|METALLIC IMPURITY(4,1)\|METHANEDIONE LONG TERM SEQUESTRATION(4,1)\|MG5CA2SI8O(4,1)\|MGO RATIO(4,1)\|MGOHCL(4,1)\|MINERAL CARBONATION(4,1)\|NEGATIVE LIMITATION REMOVING(4,1)\|NH4HCO(4,1)\|NOTATION(4,1)\|\|(US20160319395)\|ULTRAMAFIC ROCK MATERIAL(100,36)\|METAL CARBONATE(100,30)\|AERATE IMPURITY(100,9)\|SALT DECOMPOSITION(89,8)\|PURITY MAGNESITE(73,1)\|ULTRAMAFIC ROCK(54,20)\|AQUEOUS CHESHUNT MIXTURE(54,17)\|PRECIPITATOR(46,8)\|ACID RESIDUE(43,10)\|COEXTRACTION(42,1)\|METHANEDIONE(38,22)\|CHESHUNT MIXTURE(36,20)\|CR OXIDE(36,1)\|METHANEDIONE REACTION(32,2)\|AIR STRIPPER COLUMN(30,19)\|METAL SILICATE(30,8)\|RECYCLING(28,4)\|FURNACE(27,10)\|REACTOR(27,6)\|SALT HYDRATION(27,5)\|ACIDIC VAPOR(26,4)\|PRODUCING METAL CARBONATE(26,4)\|INFRASTRUCTURE(25,3)\|AQUEOUS AMMONIA MOLAR RATIO(24,2)\|ACID LEACHING(24,1)\|METAL OXIDE(21,21)\|VIEWING(20,7)\|METAL PRODUCTION(18,4)\|AMBIENT CONDITION(16,2)\|MAFIC MINERAL(15,3)\|MGCL2 6H2O HYDROLYSIS(14,1)\|GAS LIQUID PACKED COLUMN(13,7)\|ULTRAMAFIC ROCK PARTICLE(13,3)\|MGCL2 6H2O MOLE(13,1)\|PACKED SCRUBBING TOWER(13,1)\|HYDROHALIC ACID(12,3)\|CONCENTRATED SOLUTION(12,2)\|MGCL2 4H2O(12,2)\|CO2 EMISSION MITIGATION(11,1)\|NIO MNO PERCENT(11,1)\|CARBONATION REACTION(10,2)\|HEXAHYDRATE SALT(10,2)\|MAXIMAL DIMENSION(10,2)\|ACCELERATE LIBERATION(10,1)\|AQUEOUS AMMONIA FEASIBILITY(10,1)\|CHANGI WWTP(10,1)\|CO2 MINERALIZATION(10,1)\|DECOMPOSITION THERMODYNAMICS(10,1)\|GASEOUS METHANEDIONE(10,1)\|METAIGNEOUS ROCK(10,1)\|METHANEDIONE CAPTURE(10,1)\|NET CO2 CAPTURE(10,1)\|PACKING RESTRAINER(10,1)\|PASIR PANJANG(10,1)\|PULAU SAKRA(10,1)\|PULAU SERAYA(10,1)\|SINGAPORE OLEFIN(10,1)\|SMPO COGEN(10,1)\|SUBGENERIC GROUPING(10,1)\|VAPOR RECOMPRESSOR(10,1)\|ACID DIGESTION(8,2)\|AMPLE OPPORTUNITY(8,1)\|INDUSTRY INFRASTRUCTURE(8,1)\|LEACHING REQUIREMENT(8,1)\|MGCL2 2H2O(8,1)\|OPERATING COST(8,1)\|SERPENTINE ORE(8,1)\|SIMULTANEOUS EVAPORATION(8,1)\|STRATEGIC IMPORTANCE(8,1)\|MANGANESE(7,7)\|CHROMIUM(7,6)\|THERMOGRAVIMETRIC ANALYSIS(7,4)\|CO2 REMOVAL(7,3)\|COAL GASIFICATION(7,3)\|MG3SI2O(7,3)\|REEMISSION(7,3)\|AMMONIA CAPTURE(7,1)\|AQUEOUS LEACHING(7,1)\|CO2 CAPTURE REACTION(7,1)\|CO2 TON(7,1)\|CONCENTRATED LEACHATE SOLUTION(7,1)\|DIHYDRATE SALT(7,1)\|DIVERSE INDUSTRY(7,1)\|KEEPING ELECTRICITY(7,1)\|LEACHATE SOLUTION PH(7,1)\|LEACHATE STREAM(7,1)\|MG DECOMPOSITION(7,1)\|MGO MOL(7,1)\|MINERALIZATION REACTION(7,1)\|PURIFIED LEACHATE SOLUTION(7,1)\|SATURATED LEACHATE SOLUTION(7,1)\|SLOW DEHYDRATION(7,1)\|T CO2 HR TUA(7,1)\|TANK AGITATION(7,1)\|TETRAHYDRATE SALT(7,1)\|VALUE ADDED METAL SALT(7,1)\|HEATED AIR STRIPPER(6,5)\|11H2O(6,2)\|ALKALINE EARTH SILICATE MINERAL(6,2)\|EVAPORATOR(6,2)\|FIRE RETARDANT(6,2)\|HYDROGEN CHLORIDE STRIPPING(6,2)\|LAND RECLAMATION(6,2)\|METAL REFINERY(6,2)\|NEXT DECADE(6,2)\|NITROUS PRODUCT(6,2)\|HEAVY INDUSTRY(5,4)\|STEAM(5,4)\|HEATING MEDIUM(5,3)\|LEACHING(5,3)\|HSC(5,2)\|CARBONATION PRODUCT(5,1)\|COARSE SILICA SOLID RESIDUE(5,1)\|COMMERCIALIZATION(5,1)\|DESIGNED SCRUBBER(5,1)\|EFFLUENT TREATMENT(5,1)\|ELECTROLYTIC PRODUCTION(5,1)\|ESTABLISHED FUNDAMENTAL(5,1)\|GLOBAL METHANEDIONE LEVEL(5,1)\|GLOBAL SCALE(5,1)\|HARTSHORN(5,1)\|HYDRATED METAL SALT CRYSTALIZATION(5,1)\|INORGANIC SAMPLE(5,1)\|IRON OXIDATION(5,1)\|IRON SEPARATING OXIDE(5,1)\|LEACHING MEDIUM(5,1)\|LIQUID REDISTRIBUTOR(5,1)\|LISTED ITEM(5,1)\|METHANEDIONE GAS(5,1)\|NARROW SPECIES(5,1)\|NUMEROUS NITROGEN SPECIES(5,1)\|REGENERATION REACTION(5,1)\|REMOVING IMPURITY(5,1)\|SINGAPORE CHEMICAL(5,1)\|SOLID MGO RESIDUE(5,1)\|SOLUTION WARMING(5,1)\|TON CO2(5,1)\|UNCONTROLLED FORMATION(5,1)\|HYDROGEN CHLORIDE GAS(4,4)\|5H2O(4,1)\|AERATION(4,1)\|ANHYDROUS MAGNESIUM CHLORIDE(4,1)\|ASCENDING AIR(4,1)\|AUTOHYDROLYSIS DEGREE(4,1)\|AVERAGE SCALE(4,1)\|BLOWER(4,1)\|CLINOPYROXENE(4,1)\|CO2 LOSS(4,1)\|COMPARABLE SOLUTION(4,1)\|COMPLICATION FREE REGENERATION(4,1)\|CONSUMER(4,1)\|CONTAMINANT(4,1)\|CRUSHING(4,1)\|CRYSTALIZATION WATER(4,1)\|DEBACTEROL(4,1)\|DISSOLUTION HEAT(4,1)\|ELEMENT MGO(4,1)\|EXPERIMENT(4,1)\|FERRIC CHLORIDE CONVERSION(4,1)\|FILTRATE(4,1)\|GENUS(4,1)\|GIGATONNE(4,1)\|HEMATITE(4,1)\|HYDROGEN CHLORIDE REGENERATION(4,1)\|HYDROMAGNESITE(4,1)\|INSULATION(4,1)\|INTERMEDIATE SPECIES OXIDATION(4,1)\|IRON CONTENT(4,1)\|JURONG(4,1)\|KINETICS(4,1)\|LEACHING RATE(4,1)\|METAL CHLORIDE HYDROLYSIS(4,1)\|METAL LIBERATION(4,1)\|METALLIC IMPURITY(4,1)\|METHANEDIONE LONG TERM SEQUESTRATION(4,1)\|MG5CA2SI8O(4,1)\|MGCL26H2O(4,1)\|MGO RATIO(4,1)\|MGOHCL(4,1)\|MINERAL CARBONATION(4,1)\|NEGATIVE LIMITATION REMOVING(4,1)\|NH4HCO(4,1)\|NOTATION(4,1)\|\|(WO2015/099612)\|ULTRAMAFIC ROCK MATERIAL(100,28)\|METAL CARBONATE(100,23)\|AERATE IMPURITY(99,8)\|AQUEOUS AMMONIA(81,20)\|SALT DECOMPOSITION(74,6)\|PRECIPITATOR(65,8)\|AQUEOUS CHESHUNT MIXTURE(63,16)\|ULTRAMAFIC ROCK(62,19)\|AQUEOUS AMMONIA MOLAR RATIO(57,2)\|RECYCLING(53,4)\|METHANEDIONE(48,21)\|ACID RESIDUE(43,9)\|METHANEDIONE REACTION(43,3)\|CHESHUNT MIXTURE(42,20)\|MOLAR RATIO(39,6)\|AIR STRIPPER COLUMN(38,19)\|SALT HYDRATION(38,3)\|ACIDIC VAPOR(36,4)\|PACKED COLUMN(34,8)\|METAL SILICATE(32,7)\|FURNACE(31,10)\|PRODUCING METAL CARBONATE(23,3)\|GAS LIQUID PACKED COLUMN(22,7)\|AMBIENT CONDITION(22,2)\|CAO NIO MNOPERCENT(22,1)\|METAL OXIDE(20,18)\|METHANEDIONE MINERALIZATION(20,1)\|ULTRAMAFIC ROCK PARTICLE(18,3)\|PACKED SCRUBBING TOWER(18,1)\|HYDROHALIC ACID(17,3)\|SIMULTANEOUS EVAPORATION(17,2)\|METAL PRODUCTION(16,3)\|COND ITION(16,1)\|DIHYDRATE SALT UNDENVENT(16,1)\|CARBONATION REACTION(14,2)\|HEXAHYDRATE SALT(14,2)\|LIYDRATED SALT(14,2)\|MAXIMAL DIMENSION(14,2)\|ACCELERATE LIBERATION(14,1)\|AQUEOUS AMMONIA FEASIBILITY(14,1)\|COMPRESS EXITINGHCL(14,1)\|DECOMPOSITION THERMODYNAMICS(14,1)\|GASEOUS METHANEDIONE(14,1)\|HANOI WWTP(14,1)\|METHANEDIONE CAPTURE(14,1)\|PACKING RESTRAINER(14,1)\|SUBGENERIC GROUPING(14,1)\|VAPOR RECOMPRESSOR(14,1)\|ACID DIGESTION(13,3)\|AMPLE OPPORTUNITY(12,1)\|EMISSIONPOWER PLANT ENERGY(12,1)\|HR TUA(12,1)\|INDUSTRY INFRASTRUCTURE(12,1)\|LEACHING REQUIREMENT(12,1)\|MGCL HYDROLYSIS(12,1)\|SERPENTINE ORE(12,1)\|STRATEGIC IMPORTANCE(12,1)\|CANY OUT REACTION(11,2)\|MANGANESE(10,7)\|THERMOGRAVIMETRIC ANALYSIS(10,4)\|COAL GASIFICATION(10,3)\|REEMISSION(10,3)\|AMMONIA CAPTURE(10,1)\|AQUEOUS LEACHING(10,1)\|CONCENTRATED LEACHATE SOLUTION(10,1)\|DIVERSE INDUSTRY(10,1)\|HYPOCHLOROUS ACID UNDENVENT(10,1)\|KEEPING ELECTRICITY(10,1)\|LEACHATE SOLUTION PH(10,1)\|LEACHATE STREAM(10,1)\|MG DECOMPOSITION(10,1)\|MGCL2 MOLE(10,1)\|MGO MOL(10,1)\|MINERALIZATION REACTION(10,1)\|PURIFIED LEACHATE SOLUTION(10,1)\|SATURATED LEACHATE SOLUTION(10,1)\|SLOW DEHYDRATION(10,1)\|TANK AGITATION(10,1)\|TETRAHYDRATE SALT(10,1)\|CHROMIUM(9,6)\|HEATED AIR STRIPPER(9,5)\|HEAVY INDUSTRY(8,4)\|STEAM(8,4)\|ALKALINE EARTH SILICATE MINERAL(8,2)\|EVAPORATOR(8,2)\|FIRE RETARDANT(8,2)\|HYDROGEN CHLORIDE STRIPPING(8,2)\|LAND RECLAMATION(8,2)\|METAL REFINERY(8,2)\|NEXT DECADE(8,2)\|NITROUS PRODUCT(8,2)\|CARBONATION PRODUCT(8,1)\|COARSE SILICA SOLID RESIDUE(8,1)\|COMMERCIALIZATION(8,1)\|DESIGNED SCRUBBER(8,1)\|EFFLUENT TREATMENT(8,1)\|ELECTROLYTIC PRODUCTION(8,1)\|ELEMENT MGO SI(8,1)\|ESTABLISHED FUNDAMENTAL(8,1)\|EXCESS WATER CONCURRENT EVAPORATION(8,1)\|GLOBAL METHANEDIONE LEVEL(8,1)\|GLOBAL SCALE(8,1)\|HARTSHORN(8,1)\|HYDRATED METAL SALT CRYSTALIZATION(8,1)\|INORGANIC SAMPLE(8,1)\|IRON OXIDATION(8,1)\|IRON SEPARATING OXIDE(8,1)\|LEACHING MEDIUM(8,1)\|LIQUID REDISTRIBUTOR(8,1)\|LISTED ITEM(8,1)\|MAGNESIUM CHLORIDE HYDROLYSIS(8,1)\|METHANEDIONE GAS(8,1)\|NARROW SPECIES(8,1)\|NUMEROUS NITROGEN SPECIES(8,1)\|REGENERATION REACTION(8,1)\|REMOVING IMPURITY(8,1)\|SOLID MGO RESIDUE(8,1)\|SOLUTION WARMING(8,1)\|UNCONTROLLED FORMATION(8,1)\|HSC(7,2)\|HYDROGEN CHLORIDE GAS(6,4)\|HEATING MEDIUM(6,3)\|LEACHING(6,3)\|MG3SI(6,3)\|ANHYDROUS MAGNESIUM CHLORIDE(6,1)\|ASCENDING AIR(6,1)\|AUTOHYDROLYSIS DEGREE(6,1)\|AVERAGE SCALE(6,1)\|BLOWER(6,1)\|CAPTURE REACTION(6,1)\|CLINOPYROXENE(6,1)\|COMPARABLE SOLUTION(6,1)\|COMPLICATION FREE REGENERATION(6,1)\|CONSUMER(6,1)\|CONTAMINANT(6,1)\|CRUSHING(6,1)\|CRYSTALIZATION WATER(6,1)\|DEBACTEROL(6,1)\|DISSOLUTION HEAT(6,1)\|EMISSION RATE ENERGY(6,1)\|FERRIC CHLORIDE CONVERSION(6,1)\|FILTRATE(6,1)\|GENUS(6,1)\|GIGATONNE(6,1)\|HEMATITE(6,1)\|HYDROGEN CHLORIDE REGENERATION(6,1)\|HYDROMAGNESITE(6,1)\|IGNEOUS ROCK(6,1)\|INSULATION(6,1)\|INTERMEDIATE SPECIES OXIDATION(6,1)\|IRON CONTENT(6,1)\|KINETICS(6,1)\|LEACHING RATE(6,1)\|MAGNESIUMOXIDE(6,1)\|MARKUSH GROUP MEMBER(6,1)\|MERLIMAU(6,1)\|METAL CHLORIDE HYDROLYSIS(6,1)\|METAL LIBERATION(6,1)\|METALLIC IMPURITY(6,1)\|METHANEDIONE LONG TERM SEQUESTRATION(6,1)\|MG5CA2SIS(6,1)\|MGO RATIO(6,1)\|MGOHCL(6,1)\|MINERAL CARBONATION(6,1)\|MITIGATION(6,1)\|NEGATIVE LIMITATION REMOVING(6,1)\|NOTATION(6,1)\|OLIVINE(6,1)\|\|(AU2014370454)\|ULTRAMAFIC ROCK MATERIAL(100,31)\|METAL CARBONATE(100,26)\|AERATE IMPURITY(100,9)\|METAL PRODUCTION(100,3)\|PRODUCING METAL CARBONATE(100,3)\|SALT DECOMPOSITION(75,7)\|ULTRAMAFIC ROCK(54,20)\|AQUEOUS CHESHUNT MIXTURE(54,17)\|PRECIPITATOR(46,8)\|ACID RESIDUE(43,10)\|CHESHUNT MIXTURE(36,21)\|METAL SILICATE(30,8)\|METHANEDIONE REACTION(30,3)\|RECYCLING(28,4)\|FURNACE(27,10)\|REACTOR(27,6)\|SALT HYDRATION(27,5)\|AIR STRIPPER COLUMN(26,18)\|ACIDIC VAPOR(26,4)\|AQUEOUS AMMONIA MOLAR RATIO(24,2)\|METAL OXIDE(19,20)\|COGEN PASIR PANJANG(18,1)\|PULAU SAKRA SINGAPORE(18,1)\|PACKED COLUMN LIQUID(17,1)\|PULAU I1ERLIMAU ISLAND(17,1)\|AMBIENT CONDITION(16,2)\|GAS LIQUID PACKED COLUMN(15,7)\|METHANEDIONE MINERALIZATION(14,1)\|MGCL2 6H2O HYDROLYSIS(14,1)\|ULTRAMAFIC ROCK PARTICLE(13,3)\|PACKED SCRUBBING TOWER(13,1)\|HYDROHALIC ACID(12,3)\|HCI MOLE(12,2)\|HCI STRIPPING(12,2)\|CO2 EMISSION MITIGATION(11,1)\|ACID DIGESTION(10,3)\|CARBONATION REACTION(10,2)\|HEXAHYDRATE SALT(10,2)\|MAXIMAL DIMENSION(10,2)\|ACCELERATE LIBERATION(10,1)\|AQUEOUS AMMONIA FEASIBILITY(10,1)\|CO2 MINERALIZATION(10,1)\|DECOMPOSING MGC(10,1)\|DECOMPOSITION THERMODYNAMICS(10,1)\|GASEOUS METHANEDIONE(10,1)\|METAIGNEOUS ROCK(10,1)\|METHANEDIONE CAPTURE(10,1)\|NET CO2 CAPTURE(10,1)\|PACKING RESTRAINER(10,1)\|SINGAPORE OLEFIN(10,1)\|SUBGENERIC GROUPING(10,1)\|VAPOR RECOMPRESSOR(10,1)\|AMPLE OPPORTUNITY(8,1)\|ANHYDROUS MGC(8,1)\|CO2 ERNISSION ENERGY(8,1)\|INDUSTRY INFRASTRUCTURE(8,1)\|LEACHING REQUIREMENT(8,1)\|MOLTEN MGC(8,1)\|REMAINING UNREACTED HCI(8,1)\|SATURATED MGC(8,1)\|SERPENTINE ORE(8,1)\|SIMULTANEOUS EVAPORATION(8,1)\|STRATEGIC IMPORTANCE(8,1)\|MANGANESE(7,7)\|CHROMIUM(7,6)\|CO2 REMOVAL(7,3)\|COAL GASIFICATION(7,3)\|REEMISSION(7,3)\|AMMONIA CAPTURE(7,1)\|AQUEOUS LEACHING(7,1)\|CATION EXTRACTION(7,1)\|CO2 CAPTURE REACTION(7,1)\|CO2 TON(7,1)\|CONCENTRATED LEACHATE SOLUTION(7,1)\|DIHYDRATE SALT(7,1)\|DIVERSE INDUSTRY(7,1)\|FEC CONVERSION(7,1)\|KEEPING ELECTRICITY(7,1)\|LEACHATE SOLUTION PH(7,1)\|LEACHATE STREAM(7,1)\|MG DECOMPOSITION(7,1)\|MGC MOLE(7,1)\|MGO MOL(7,1)\|MINERALIZATION REACTION(7,1)\|PURIFIED LEACHATE SOLUTION(7,1)\|SATURATED LEACHATE SOLUTION(7,1)\|SLOW DEHYDRATION(7,1)\|TANK AGITATION(7,1)\|TETRAHYDRATE SALT(7,1)\|HEATED AIR STRIPPER(6,5)\|ALKALINE EARTH SILICATE MINERAL(6,2)\|EVAPORATOR(6,2)\|FIRE RETARDANT(6,2)\|LAND RECLAMATION(6,2)\|METAL REFINERY(6,2)\|NEXT DECADE(6,2)\|NITROUS PRODUCT(6,2)\|HEAVY INDUSTRY(5,4)\|STEAM(5,4)\|EXCESS WATER(5,3)\|FERRIC CHLORIDE(5,3)\|HEATING MEDIUM(5,3)\|LEACHING(5,3)\|THERMOGRAVIMETRIC ANALYSIS(5,3)\|HSC(5,2)\|CARBONATION PRODUCT(5,1)\|CO2 EMISSION RATE(5,1)\|COARSE SILICA SOLID RESIDUE(5,1)\|COMMERCIALIZATION(5,1)\|DESIGNED SCRUBBER(5,1)\|EFFLUENT TREATMENT(5,1)\|ELECTROLYTIC PRODUCTION(5,1)\|ENERGY CO2 EMISSION(5,1)\|ESTABLISHED FUNDAMENTAL(5,1)\|GLOBAL METHANEDIONE LEVEL(5,1)\|GLOBAL SCALE(5,1)\|H2O FE(5,1)\|HARTSHORN(5,1)\|HYDRATED METAL SALT CRYSTALIZATION(5,1)\|INORGANIC SAMPLE(5,1)\|IRON OXIDATION(5,1)\|IRON SEPARATING OXIDE(5,1)\|LEACHING MEDIUM(5,1)\|LIQUID REDISTRIBUTOR(5,1)\|LISTED ITEM(5,1)\|MAGNESIUM CHLORIDE HEXAHYDRATE HYDROLYSIS(5,1)\|METHANEDIONE GAS(5,1)\|NARROW SPECIES(5,1)\|NUMEROUS NITROGEN SPECIES(5,1)\|REGENERATION REACTION(5,1)\|REMOVING IMPURITY(5,1)\|SOLID MGO RESIDUE(5,1)\|SOLUTION WARMING(5,1)\|TON CO2(5,1)\|UNCONTROLLED FORMATION(5,1)\|AERATION(4,1)\|ASCENDING AIR(4,1)\|AUTOHYDROLYSIS DEGREE(4,1)\|AVERAGE SCALE(4,1)\|BLOWER(4,1)\|CLINOPYROXENE(4,1)\|CO2 LOSS(4,1)\|COMPARABLE SOLUTION(4,1)\|COMPLICATION FREE REGENERATION(4,1)\|CONSUMER(4,1)\|CONTAMINANT(4,1)\|CRUSHING(4,1)\|CRYSTALIZATION WATER(4,1)\|DEBACTEROL(4,1)\|DISSOLUTION HEAT(4,1)\|FILTRATE(4,1)\|GENUS(4,1)\|GIGATONNE(4,1)\|HEMATITE(4,1)\|HYDROMAGNESITE(4,1)\|INSULATION(4,1)\|INTERMEDIATE SPECIES OXIDATION(4,1)\|IRON CONTENT(4,1)\|KINETICS(4,1)\|LEACHING RATE(4,1)\|METAL CHLORIDE HYDROLYSIS(4,1)\|METAL LIBERATION(4,1)\|METALLIC IMPURITY(4,1)\|METHANEDIONE LONG TERM SEQUESTRATION(4,1)\|MG3SI2O(4,1)\|MG5CA2SI(4,1)\|MGO RATIO(4,1)\|MINERAL CARBONATION(4,1)\|NEGATIVE LIMITATION REMOVING(4,1)\|NH4HCO(4,1)\|NOTATION(4,1)\|OLIVINE(4,1)\|\|(AU2014370454)\|ULTRAMAFIC ROCK MATERIAL(100,31)\|METAL CARBONATE(100,26)\|AERATE IMPURITY(100,9)\|METAL PRODUCTION(100,3)\|PRODUCING METAL CARBONATE(100,3)\|SALT DECOMPOSITION(75,7)\|ULTRAMAFIC ROCK(54,20)\|AQUEOUS CHESHUNT MIXTURE(54,17)\|PRECIPITATOR(46,8)\|ACID RESIDUE(43,10)\|CHESHUNT MIXTURE(36,21)\|METAL SILICATE(30,8)\|METHANEDIONE REACTION(30,3)\|RECYCLING(28,4)\|FURNACE(27,10)\|REACTOR(27,6)\|SALT HYDRATION(27,5)\|AIR STRIPPER COLUMN(26,18)\|ACIDIC VAPOR(26,4)\|AQUEOUS AMMONIA MOLAR RATIO(24,2)\|METAL OXIDE(19,20)\|COGEN PASIR PANJANG(18,1)\|PULAU SAKRA SINGAPORE(18,1)\|PACKED COLUMN LIQUID(17,1)\|PULAU I1ERLIMAU ISLAND(17,1)\|AMBIENT CONDITION(16,2)\|GAS LIQUID PACKED COLUMN(15,7)\|METHANEDIONE MINERALIZATION(14,1)\|MGCL2 6H2O HYDROLYSIS(14,1)\|ULTRAMAFIC ROCK PARTICLE(13,3)\|PACKED SCRUBBING TOWER(13,1)\|HYDROHALIC ACID(12,3)\|HCI MOLE(12,2)\|HCI STRIPPING(12,2)\|CO2 EMISSION MITIGATION(11,1)\|ACID DIGESTION(10,3)\|CARBONATION REACTION(10,2)\|HEXAHYDRATE SALT(10,2)\|MAXIMAL DIMENSION(10,2)\|ACCELERATE LIBERATION(10,1)\|AQUEOUS AMMONIA FEASIBILITY(10,1)\|CO2 MINERALIZATION(10,1)\|DECOMPOSING MGC(10,1)\|DECOMPOSITION THERMODYNAMICS(10,1)\|GASEOUS METHANEDIONE(10,1)\|METAIGNEOUS ROCK(10,1)\|METHANEDIONE CAPTURE(10,1)\|NET CO2 CAPTURE(10,1)\|PACKING RESTRAINER(10,1)\|SINGAPORE OLEFIN(10,1)\|SUBGENERIC GROUPING(10,1)\|VAPOR RECOMPRESSOR(10,1)\|AMPLE OPPORTUNITY(8,1)\|ANHYDROUS MGC(8,1)\|CO2 ERNISSION ENERGY(8,1)\|INDUSTRY INFRASTRUCTURE(8,1)\|LEACHING REQUIREMENT(8,1)\|MOLTEN MGC(8,1)\|REMAINING UNREACTED HCI(8,1)\|SATURATED MGC(8,1)\|SERPENTINE ORE(8,1)\|SIMULTANEOUS EVAPORATION(8,1)\|STRATEGIC IMPORTANCE(8,1)\|MANGANESE(7,7)\|CHROMIUM(7,6)\|CO2 REMOVAL(7,3)\|COAL GASIFICATION(7,3)\|REEMISSION(7,3)\|AMMONIA CAPTURE(7,1)\|AQUEOUS LEACHING(7,1)\|CATION EXTRACTION(7,1)\|CO2 CAPTURE REACTION(7,1)\|CO2 TON(7,1)\|CONCENTRATED LEACHATE SOLUTION(7,1)\|DIHYDRATE SALT(7,1)\|DIVERSE INDUSTRY(7,1)\|FEC CONVERSION(7,1)\|KEEPING ELECTRICITY(7,1)\|LEACHATE SOLUTION PH(7,1)\|LEACHATE STREAM(7,1)\|MG DECOMPOSITION(7,1)\|MGC MOLE(7,1)\|MGO MOL(7,1)\|MINERALIZATION REACTION(7,1)\|PURIFIED LEACHATE SOLUTION(7,1)\|SATURATED LEACHATE SOLUTION(7,1)\|SLOW DEHYDRATION(7,1)\|TANK AGITATION(7,1)\|TETRAHYDRATE SALT(7,1)\|HEATED AIR STRIPPER(6,5)\|ALKALINE EARTH SILICATE MINERAL(6,2)\|EVAPORATOR(6,2)\|FIRE RETARDANT(6,2)\|LAND RECLAMATION(6,2)\|METAL REFINERY(6,2)\|NEXT DECADE(6,2)\|NITROUS PRODUCT(6,2)\|HEAVY INDUSTRY(5,4)\|STEAM(5,4)\|EXCESS WATER(5,3)\|FERRIC CHLORIDE(5,3)\|HEATING MEDIUM(5,3)\|LEACHING(5,3)\|THERMOGRAVIMETRIC ANALYSIS(5,3)\|HSC(5,2)\|CARBONATION PRODUCT(5,1)\|CO2 EMISSION RATE(5,1)\|COARSE SILICA SOLID RESIDUE(5,1)\|COMMERCIALIZATION(5,1)\|DESIGNED SCRUBBER(5,1)\|EFFLUENT TREATMENT(5,1)\|ELECTROLYTIC PRODUCTION(5,1)\|ENERGY CO2 EMISSION(5,1)\|ESTABLISHED FUNDAMENTAL(5,1)\|GLOBAL METHANEDIONE LEVEL(5,1)\|GLOBAL SCALE(5,1)\|H2O FE(5,1)\|HARTSHORN(5,1)\|HYDRATED METAL SALT CRYSTALIZATION(5,1)\|INORGANIC SAMPLE(5,1)\|IRON OXIDATION(5,1)\|IRON SEPARATING OXIDE(5,1)\|LEACHING MEDIUM(5,1)\|LIQUID REDISTRIBUTOR(5,1)\|LISTED ITEM(5,1)\|MAGNESIUM CHLORIDE HEXAHYDRATE HYDROLYSIS(5,1)\|METHANEDIONE GAS(5,1)\|NARROW SPECIES(5,1)\|NUMEROUS NITROGEN SPECIES(5,1)\|REGENERATION REACTION(5,1)\|REMOVING IMPURITY(5,1)\|SOLID MGO RESIDUE(5,1)\|SOLUTION WARMING(5,1)\|TON CO2(5,1)\|UNCONTROLLED FORMATION(5,1)\|AERATION(4,1)\|ASCENDING AIR(4,1)\|AUTOHYDROLYSIS DEGREE(4,1)\|AVERAGE SCALE(4,1)\|BLOWER(4,1)\|CLINOPYROXENE(4,1)\|CO2 LOSS(4,1)\|COMPARABLE SOLUTION(4,1)\|COMPLICATION FREE REGENERATION(4,1)\|CONSUMER(4,1)\|CONTAMINANT(4,1)\|CRUSHING(4,1)\|CRYSTALIZATION WATER(4,1)\|DEBACTEROL(4,1)\|DISSOLUTION HEAT(4,1)\|FILTRATE(4,1)\|GENUS(4,1)\|GIGATONNE(4,1)\|HEMATITE(4,1)\|HYDROMAGNESITE(4,1)\|INSULATION(4,1)\|INTERMEDIATE SPECIES OXIDATION(4,1)\|IRON CONTENT(4,1)\|KINETICS(4,1)\|LEACHING RATE(4,1)\|METAL CHLORIDE HYDROLYSIS(4,1)\|METAL LIBERATION(4,1)\|METALLIC IMPURITY(4,1)\|METHANEDIONE LONG TERM SEQUESTRATION(4,1)\|MG3SI2O(4,1)\|MG5CA2SI(4,1)\|MGO RATIO(4,1)\|MINERAL CARBONATION(4,1)\|NEGATIVE LIMITATION REMOVING(4,1)\|NH4HCO(4,1)\|NOTATION(4,1)\|OLIVINE(4,1)\|	(US9896741)\|The invention claimed is:\|1. A method of producing a metal carbonate from an ultramafic rock material, the method comprising\| a) providing an ultramafic rock material comprising a metal silicate;\| b) reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| c) contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| d) heating the resultant mixture from step c) to decompose the salt of the metal to form metal oxide; and\| e) reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|2. The method according to claim 1, wherein molar ratio of metal to CO3 in the metal carbonate is in the range of about 1:1 to about 5:4.\|3. The method according to claim 1, wherein the metal carbonate is magnesium carbonate.\|4. The method according to claim 1, wherein the ultramafic rock material comprises serpentine.\|5. The method according to claim 1, wherein the acid is a hydrohalic acid.\|6. The method according to claim 1, wherein the acid comprises hydrochloric acid.\|7. The method according to claim 6, wherein concentration of the hydrochloric acid is at least 27 wt % HCl.\|8. The method according to claim 1, wherein reacting the ultramafic rock material with an acid is carried out at a temperature in the range of about 80° C. to about 100° C.\|9. The method according to claim 1, wherein contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature in the range of about 150° C. to about 250° C.\|10. The method according to claim 1, wherein contacting the mixture comprising a salt of the metal with oxygen is carried out under conditions such that pH of the mixture is less than or equal to 9.\|11. The method according to claim 1, wherein contacting the mixture comprising a salt of the metal with oxygen is carried out for a time period suitable to form a mixture saturated with the salt.\|12. The method according to claim 1, further comprising removing water from the resultant mixture from step c) prior to step d) to form a hydrated salt of the metal.\|13. The method according to claim 1, wherein reacting the metal oxide with aqueous ammonium carbonate is carried out at ambient conditions.\|14. The method according to claim 1, wherein the aqueous ammonium carbonate is obtained by reacting carbon dioxide with aqueous ammonia in a gas-liquid packed column.\|15. The method according to claim 14, wherein molar ratio of aqueous ammonia to carbon dioxide is in the range of about 2:1 to about 2.5:1.\|16. A system for producing a metal carbonate from ultramafic rock material, the system comprising\| a) a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| b) an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| c) a furnace configured to heat the resultant mixture from step b) to decompose the salt of the metal to form the metal oxide; and\| d) a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|17. The system according to claim 16, further comprising a gas-liquid packed column arranged upstream of the precipitator and configured to carry out reaction of carbon dioxide with aqueous ammonia to form aqueous ammonium carbonate.\|18. The system according to claim 17, further comprising recycling means configured to recycle aqueous ammonia from the precipitator to the gas-liquid packed column.\|19. The system according to claim 16, further comprising a compressor configured to compress acid vapor and/or water vapor from the air stripper column.\|20. The system according to claim 16, further comprising recycling means configured to recycle acid vapor and/or water vapor from the air stripper column and/or the furnace to the reactor and/or the air stripper column.	(US9896741)\|TECHNICAL FIELD\|[0002] The invention relates to methods of producing metal carbonate from an ultramafic rock material.\|BACKGROUND\|[0003] Heavy industries such as steel making, coal gasification, metal refineries, power plants and cement making units emit a significant amount of carbon dioxide (CO2). Taking Singapore, for example, it was estimated that amount of carbon dioxide from power plants will exceed 20 million tonnes per year for the next decade (see TABLE 1).\|[0004] TABLE 1 Carbon dioxide (CO2) emissions from power plants in Singapore (2007-2017) 2007 Energy and CO2 Emission2017 Energy and CO2 Emission CO2Emission CO2Emission EnergyEmissionrateEnergyEmissionratePower PlantMWh/aMt CO2/at CO2/hrMWh/aMt CO2/at CO2/hr TUAS8,867,2754.0045717,100,00013.201507PULAU SERAYA8,297,8683.9344813,000,0006.00685SENOKO11,200,0004.4550811,500,0004.56520PULAU MERLIMAU0 2,931,1241.29147ISLAND POWER0 2,537,8751.27145PULAU SAKRA2,090,1030.871002,177,4970.91104SINGAPORE CHEMICAL684,5770.38431,610,5930.8395JURONG325,7140.1518363,8600.1719SINGAPORE OLEFINS318,4060.1517332,2270.1618CHANGI WWTP257,3030.1214276,9990.1315SMPO COGEN173,3210.1112182,3920.1113PASIR PANJANG185,0810.0910200,6640.1011Total32,399,64814.3 52,213,23028.7 Source: http://carma.org/region/detail/169\|[0005] Carbon dioxide capture and storage by mineralization has been proposed as a possible technology to reduce global carbon dioxide levels. The technology may include extracting cations from feed material such as rocks, and combining the cations with carbon dioxide to form a stable carbonate material. Due to the large quantities (gigatonnes) of material involved, ability to extract metal from the feed material at high efficiencies is important. Limitations to existing processes include low metal extraction yields and high energy consumption, due to removal of water which has high latent and sensible heat.\|[0006] In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|SUMMARY\|[0007] In a first aspect, a method of producing a metal carbonate from an ultramafic rock material is provided. The method comprises\| - a) providing an ultramafic rock material comprising a metal silicate;\| - b) reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| - c) contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| - d) heating the resultant mixture from step c) to decompose the salt of the metal to form metal oxide; and\| - e) reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|[0013] In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided. The system comprises\| - a) a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| - b) an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| - c) a furnace configured to heat the resultant mixture from step b) to decompose the salt of the metal to form the metal oxide; and\| - d) a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to form the metal carbonate.\|(US9896741)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] The invention will be better understood with reference to the detailed description when considered in conjunction with the non-limiting examples and the accompanying drawings, in which:\|[0019] FIG. 1 is a schematic diagram depicting working mechanism of an air stripper column. Notations in the figures represent the following: 101: packed column; 102: packing material; 103: packing support; 104: packing restrainer; 105: liquid redistributors; 106: blower assembly; 111: contaminant influent; 112: spray; 113: air in; 114: gas out to atmosphere or secondary treatment; and 115: treated effluent.\|[0020] FIG. 2 is a schematic diagram showing process flow for a mineralization process according to an embodiment.\|[0021] FIG. 3 is a graph showing thermogravimetric analysis (TGA) results of MgCl2.6H2O. Y-axis: weight; x-axis: temperature (° C.).\|[0022] FIG. 4 is a graph showing TGA analysis of magnesium carbonate product from reaction of MgO with (NH4)2CO3. Y-axis: weight (mg); x-axis: temperature (° C.).\|[0023] FIG. 5 is a schematic diagram showing general process flow for a system to carry out mineralization process according to embodiments.\|(US9896741)\|DETAILED DESCRIPTION\|[0024] Using methods disclosed herein, carbon dioxide emitted from various sources, such as coal gasification and power plants, may be captured in the form of metal carbonates such as magnesium carbonate, without significant modification of existing infrastructure. The metal carbonates are thermodynamically stable and inert, and once bound, the carbon dioxide that is captured is not susceptible to re-emission into the atmosphere. Furthermore, the metal carbonates produced may be in solid form to render their ease of handling.\|[0025] Various embodiments disclosed herein are particularly suited for long-term sequestration of carbon dioxide emitted from industries. Advantageously, systems for producing metal carbonate disclosed herein may be integrated into existing infrastructure of industries so as to utilize waste heat from the industries in production of metal carbonates. The metal carbonates produced may be used as building materials or for land reclamation purposes, or be used as additives for adding to polymers as fire retardants.\|[0026] With the above in mind, various embodiments refer in a first aspect to a method of producing a metal carbonate from an ultramafic rock material.\|[0027] The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|[0028] As used herein, the term “ultramafic rock material” refers to igneous and meta-igneous rocks which are composed of more than 90% mafic minerals in various proportions with trace amounts of other minerals. The term “mafic” is used to describe a silicate mineral or rock that is rich in magnesium. Apart from magnesium, the ultramafic rock material may also contain metals such as iron, nickel, chromium, manganese and/or calcium as impurities.\|[0029] Main mafic minerals include olivine (Mg2SiO4), orthopyroxene (MgSiO3), and clinopyroxene ((MgCa)SiO3). Upon hydration, the corresponding mafic minerals are serpentine (Mg3Si2O5(OH)4), tremolite (Mg5Ca2Si8O22(OH)2), and talc (Mg3Si4O10(OH)2).\|[0030] Of particular importance is serpentine, as it is volumetrically dominant on a global scale. Typically, serpentine has a silica content of less than 45%, magnesium oxide content of greater than 18%, and a high iron oxide content in the range of about 5% to 15%. Content of serpentine may vary between the stated ranges depending on source and quality of the rock. TABLE 2 depicts composition of serpentine according to an embodiment. The values are obtained from direct measurements of the mineral samples using X-ray fluorescence spectroscopy.\|[0031] TABLE 2 Composition of Serpentine (Percentage expressed in terms of weight% of the respective oxides contained within the material)ElementMgOSiO2Fe2O3Al2O3Cr2O3CaONiOMnO Percent46.7242.78.40.610.450.40.290.14 \|[0032] In various embodiments, the ultramafic rock material comprises or consists of serpentine.\|[0033] As mentioned above, the ultramafic rock material is rich in magnesium. Accordingly, in various embodiments, the method of producing metal carbonate from an ultramafic rock material is used to produce magnesium carbonate. Molar ratio of metal to carbonate (CO3) in the metal carbonate may be in the range of about 1:1 to about 5:4. In various embodiments, molar ratio of metal to CO3 in the metal carbonate is about 1:1.\|[0034] The method includes providing an ultramafic rock material comprising a metal silicate. In various embodiments, the metal silicate is magnesium silicate, such as Mg3Si2O5(OH)4. Apart from magnesium silicate, silicates of other metals contained in the ultramafic rock material may also be present, such as silicates of iron, nickel, chromium, manganese, and/or calcium.\|[0035] Providing an ultramafic rock material comprising a metal silicate may include physically working the ultramafic rock material such as by crushing or grinding, so as to reduce size of the ultramafic rock material. Advantageously, by reducing size of the ultramafic rock material, liberation of metal from the ultramafic rock material may be accelerated.\|[0036] In some embodiments, providing an ultramafic rock material includes physically working the ultramafic rock material to form ultramafic rock particles having a size of 0.5 mm or less. Size of the ultramafic rock particles may be characterized by its maximal dimension, wherein the term “maximal dimension” refers to the maximal length of a straight line segment passing through the center of a figure and terminating at the periphery.\|[0037] For example, the ultramafic rock material may comprise or consist of ultramafic rock particles having a size of 0.5 mm or less, such as a size in the range of about 0.01 mm to about 0.5 mm, about 0.05 mm to about 0.5 mm, about 0.1 mm to about 0.5 mm, about 0.2 mm to about 0.5 mm, about 0.01 mm to about 0.3 mm, about 0.01 mm to about 0.1 mm, or about 0.1 mm to about 0.3 mm.\|[0038] The method includes reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal. In reacting the ultramafic rock material with an acid, metal from the ultramafic rock material may be leached out in the form of a metal salt. Hence, the mixture containing the salt of the metal may otherwise be termed as the leachate. A solid residue of coarse silica may also be obtained following reacting of the ultramafic rock material with acid.\|[0039] The acid may, for example, be selected from the group consisting of hydrohalic acid, sulfuric acid (H2SO4), nitric acid (HNO3), phosphoric acid (H3PO4), acetic acid (CH3COOH), and combinations thereof. Depending on the acid used, different metal salts may be formed. For example, salt of the metal may be a halide such as a chloride or a bromide, a sulfate, a nitrate, a phosphate, and/or an acetate. In various embodiments, the acid is a hydrohalic acid, such as hydrofluoric acid (HF), hydrochloric acid (HCl), hydrobromic acid (HBr), and/or hydroiodic acid (HI). In some embodiments, the acid comprises or consists of hydrochloric acid and/or hydrobromic acid.\|[0040] In specific embodiments, the acid comprises or consists of hydrochloric acid. By reacting the ultramafic rock material with hydrochloric acid, metal may be leached from the ultramafic rock material as metal chloride. Use of hydrochloric acid has been found by the inventors to be advantageous, as hydrochloric acid is able to leach metal effectively from ultramafic rock material, and may be regenerated easily and simply without complication. Undesirable decompositions do not take place upon heating of metal chlorides, as opposed to the case of metal nitrates formed from reacting metal silicates with nitric acid, for example, which may generate nitrite and nitrous products.\|[0041] The mixture may accordingly contain chlorides of magnesium, iron, nickel, chromium, manganese, and/or calcium. Due to the high magnesium content in ultramafic rock material, the salt of the metal may mainly be made up of magnesium chloride.\|[0042] In various embodiments, concentration of the hydrochloric acid is at least 27 wt % HCl. For example, concentration of the hydrochloric acid may be at least 30 wt %, at least 35 wt % HCl, or be in the range of about 27 wt % to about 35 wt %, about 27 wt % to about 32 wt %, or about 27 wt % to about 30 wt % HCl.\|[0043] Reacting the ultramafic rock material with an acid may be carried out at a temperature in the range of about 80° C. to about 100° C. For example, reacting the ultramafic rock material with an acid may be carried out at a temperature in the range of about 80° C. to about 95° C., about 80° C. to about 90° C., about 80° C. to about 85° C., about 90° C. to about 100° C., or about 85° C. to about 95° C. In various embodiments, reacting the ultramafic rock material with an acid is carried out under continuous stirring to accelerate liberation of metal from the ultramafic rock material.\|[0044] The method includes contacting the mixture comprising a salt from the metal with oxygen. The oxygen may be in the form of an oxygen flow and/or an air flow. This may be carried out to aerate impurities in the mixture and/or to remove residual acid from the mixture. As mentioned above, the ultramafic rock material may also contain metals such as iron, nickel, chromium, manganese and/or calcium as impurities. By contacting the mixture comprising a salt of the metal with oxygen, the metals may be aerated to their respective oxides and may be precipitated out from the mixture to allow their removal from the resultant mixture by a separation process such as decanting or filtering.\|[0045] By way of example only, this aeration process may be illustrated using hydrochloric acid and iron. Iron may be leached from ultramafic rock material using hydrochloric acid to form iron (II) chloride (FeCl2). The iron (II) chloride may be oxidized readily to iron (III) chloride (FeCl3) upon contact with oxygen, as shown in equation (1):\|12FeCl2+3O2→2Fe2O3+8FeCl3 (1)\|[0046] The iron (III) chloride may undergo auto-hydrolysis in solution to form iron (III) oxide and hydrogen chloride, as shown in equation (2):\|2FeCl3+3H2O→Fe2O3+6HCl (2)\|[0047] Iron (III) oxide may be precipitated out from the mixture following oxidation to allow their easy removal.\|[0048] In various embodiments, contacting the mixture comprising a salt of the metal with oxygen to aerate impurities in the mixture comprises separating oxides of iron, nickel, chromium, aluminum and/or manganese from the resultant mixture following oxidation.\|[0049] Further, from equation (2), it may be seen that by eliminating hydrochloric acid from the solution, conversion of iron (III) chloride into iron (III) oxide may be promoted. This means that metal impurities in the mixture may be removed to a greater extent by removing hydrochloric acid from the mixture. Advantageously, the removal of hydrochloric acid, which may arise from the auto-hydrolysis process as well as residual acid present in the mixture, may be carried out by contacting the mixture comprising a salt of the metal with oxygen.\|[0050] Contacting the mixture comprising a salt of the metal with oxygen may be carried out in a flow of air and/or oxygen. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out by air stripping. As used herein, the term “air stripping” refers to a process by which an air stream is used to remove dissolved gases or volatile components of a liquid. The air stripping may be carried out in an air stripper column. For example, the mixture comprising a salt of the metal may be introduced at the top of an air stripper column. The air stripper column may contain packing material to provide a larger contact surface area for aeration. Air may be introduced at the bottom of the air stripper column, such that the mixture flows in opposite direction to the ascending air while contacting each other. In so doing, the air may strip acid from the mixture. The air exits from the top of the air stripper column, while the resultant mixture, which has been at least partially stripped of acid, may leave the bottom of the air stripper column for channeling into a subsequent stage.\|[0051] In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out under conditions such that pH of the mixture is less than or equal to 9. For example, the contacting may be carried out under conditions such that pH of the mixture is in the range of about 3 to about 9, about 5 to about 9, about 7 to about 9, about 3 to about 7, about 3 to about 5, about 5 to about 7, or about 4 to about 6.\|[0052] Contacting the mixture comprising a salt of the metal with oxygen may be carried out at a temperature in the range of about 150° C. to about 250° C., such as about 180° C. to about 250° C., about 200° C. to about 250° C., about 150° C. to about 220° C., about 150° C. to about 200° C., about 180° C. to about 220° C., or about 180° C. to about 200° C. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature in the range of about 180° C. to about 200° C. In some embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature of about 200° C.\|[0053] By contacting the mixture comprising a salt of the metal with oxygen at elevated temperatures, water may be evaporated or vaporized from the mixture to form steam. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out for a time period suitable to form a mixture saturated with the salt. Advantageously, by removing water from the mixture, this minimizes water content in the mixture for removal in a subsequent stage. At the same time, heat energy may be recovered in the form of steam for rechanneling back into the process.\|[0054] By removing water from the mixture, a hydrated salt of the metal may also be formed. In various embodiments, the hydrated salt of the metal comprises or consists essentially of magnesium chloride hydrates. Water of crystallization of the hydrated metal salt may be in the range of about 2 to about 6, such as 2, 3, 4, 5, or 6.\|[0055] The method of the first aspect includes heating the resultant mixture following contact with oxygen to decompose the salt of the metal to form metal oxide. For example, the metal oxide may contain magnesium oxide, along with trace amounts of oxides of iron, nickel, chromium, manganese, and/or calcium which may not have been removed in an earlier stage.\|[0056] In various embodiments, heating the resultant mixture is carried out at a temperature in the range of about 400° C. to about 600° C., such as about 450° C. to about 600° C., about 500° C. to about 600° C., about 550° C. to about 600° C., about 400° C. to about 550° C., or about 450° C. to about 550° C. In specific embodiments, heating the resultant mixture is carried out at a temperature of about 550° C.\|[0057] Given the high temperatures, steam may be generated. In embodiments where the acid is hydrochloric acid, and where residual acid is present in the resultant mixture not removed in an earlier stage, hydrogen chloride gas may additionally be produced.\|[0058] The metal oxide is reacted with aqueous ammonium carbonate to obtain the metal carbonate. At the same time, aqueous ammonia may be produced.\|[0059] The aqueous ammonium carbonate may be obtained by reacting carbon dioxide with aqueous ammonia, which may be carried out in a gas-liquid packed column. The carbon dioxide may be comprised in a flue gas, which may be channeled from heavy industries such as a power plant.\|[0060] Molar ratio of aqueous ammonia to carbon dioxide may be in the range of about 2:1 to about 2.5:1, such as about 2.1:1, 2.2:1, 2.3:1, 2,4:1, or about 2.5:1.\|[0061] In various embodiments, reacting carbon dioxide with aqueous ammonia is carried out at a pH of at least 9 to maximize degree of carbonation. For example, reacting carbon dioxide with aqueous ammonia may be carried out at a pH in the range of about 9 to about 13, about 9 to about 12, about 9 to about 11, about 9 to about 10, about 10 to about 13, about 11 to about 13, or about 10 to about 12. In some embodiments, reacting carbon dioxide with aqueous ammonia is carried out at a pH of at least 10.\|[0062] Advantageously, reacting the metal oxide with aqueous ammonium carbonate may be carried out at ambient conditions.\|[0063] In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided. The system comprises a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal; an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen to aerate impurities in the mixture and/or to remove residual acid from the mixture; a furnace configured to heat the resultant mixture to decompose the salt of the metal to form the metal oxide; and a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. Schematic diagram of a system for producing a metal carbonate from ultramafic rock material according to embodiments is shown in FIG. 5 and discussed in Example 8. Processing conditions for operating the various components of the system have already been discussed above.\|[0064] In various embodiments, the system further comprises a gas-liquid packed column arranged upstream of the precipitator and configured to carry out reaction of carbon dioxide with aqueous ammonia to form aqueous ammonium carbonate. As mentioned above, the carbon dioxide may be comprised in a flue gas, which may be channeled from heavy industries such as a power plant. The ammonium carbonate that is formed may be used to react with the metal oxide to form metal carbonate. In so doing, carbon dioxide may be captured in the metal carbonate which is thermodynamically stable and inert, thereby rendering the carbon dioxide that is captured not susceptible for re-emission into the atmosphere.\|[0065] The system may further comprise a compressor configured to compress acid vapor and/or water vapor from the air stripper column. This allows formation of higher quality steam that may be used to supplement heating medium that may be used for operating the air stripper column.\|[0066] The system may, in various embodiments, comprise recycling means configured to recycle acid vapor and/or water vapor from the air stripper column and/or the furnace to the reactor and/or the air stripper column. In so doing, heat energy that is generated from the air stripper column and/or the furnace may be reused in other parts of the process, thereby minimizing energy consumption of the system.\|[0067] In various embodiments, the system further comprises recycling means configured to recycle aqueous ammonia from the precipitator to the gas-liquid packed column. As mentioned above, metal oxide may be reacted with aqueous ammonium carbonate to obtain metal carbonate in the precipitator, while producing aqueous ammonia at the same time. By recycling the aqueous ammonia produced to the gas-liquid packed column, the aqueous ammonia may be reused to react with carbon dioxide to form aqueous ammonium carbonate.\|[0068] Hereinafter, the present invention will be described more fully with reference to the accompanying drawings, in which exemplary embodiments of the invention are shown. This invention may, however, be embodied in many different forms and should not be construed as limited to the exemplary embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art. In the drawings, lengths and sizes of layers and regions may be exaggerated for clarity.\|[0069] As used herein, the term “and/or” includes any and all combinations of one or more of the associated listed items. The invention illustratively described herein may suitably be practiced in the absence of any element or elements, limitation or limitations, not specifically disclosed herein. Thus, for example, the terms “comprising”, “including”, “containing”, etc. shall be read expansively and without limitation. Additionally, the terms and expressions employed herein have been used as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the invention claimed. Thus, it should be understood that although the present invention has been specifically disclosed by preferred embodiments and optional features, modification and variation of the inventions embodied therein herein disclosed may be resorted to by those skilled in the art, and that such modifications and variations are considered to be within the scope of this invention.\|[0070] The invention has been described broadly and generically herein. Each of the narrower species and subgeneric groupings falling within the generic disclosure also form part of the invention. This includes the generic description of the invention with a proviso or negative limitation removing any subject matter from the genus, regardless of whether or not the excised material is specifically recited herein.\|[0071] Other embodiments are within the following claims and non-limiting examples. In addition, where features or aspects of the invention are described in terms of Markush groups, those skilled in the art will recognize that the invention is also thereby described in terms of any individual member or subgroup of members of the Markush group.\|EXPERIMENTAL SECTION\|[0072] Various embodiments described herein relate to a process to convert gaseous carbon dioxide from flue gas into a mineralized form, bound to alkaline earth metals obtained from ultramafic rocks. A general overall equation, employing serpentine (Mg3Si2O5(OH)4) as a representative starting material, to describe the process is as follows:\|Mg3Si2O5(OH)4+3CO2→3MgCO3+2SiO2+2H2O\|[0073] The carbon dioxide is converted into a carbonate, which is thermodynamically more stable and inert. The solid form of the carbonate is easily handled and once bound, the carbon dioxide is not susceptible to re-emission into the atmosphere unless subjected to extreme conditions.\|[0074] Improvements over state-of-the-art mineralization routes include:\|[0075] a) lower energy consumption—It is readily apparent that the net CO2 capture amount for the process described herein is positive, at least in cases where natural gas and oil are the preferred fossil fuels for combustion. This cannot be said for state of the art mineralization processes. The utilization of direct thermal energy significantly contributes to much lower CO2 emissions per ton CO2 captured. In the case of Singapore, which utilizes natural gas as the preferred fuel of choice for power generation, every 2,500 kWh produces one ton of CO2. The amount of CO2 avoided in this case is around 30%, if other assorted electrical energy uses (such as for agitation, milling, and pumping) are taken into account.\|[0076] b) established fundamentals of reactions—kinetics and thermodynamics of decomposition, as well as processes of producing anhydrous MgCl2 have been studied as MgCl2 is an important precursor to electrolytic production of magnesium metal, and thus is of strategic importance.\|[0077] c) avoidance of messy and uncontrollable side reactions—one distinct advantage of using an HCl as a leaching medium is that the regeneration reaction to yield acid is relatively uncomplicated. There are no unwanted secondary decompositions when heating is applied, unlike when nitrates are involved (there is a possibility of nitrite and nitrous products forming when pyrolysis of the nitrate salt occurs).\|[0078] d) relatively small reactor sizes—the scale of operations, when it comes to carbon capture, often involves millions of tons of material being conveyed and pumped annually. Thus, it is desirable to use concentrated solutions or gases in order to reduce infrastructure and operating costs. In fact, one may even argue that a more concentrated solution facilitates certain steps in the process, such as the evaporation stages. Since magnesium chloride is highly soluble in water, a very concentrated leachate solution may be obtained, and thus only relatively small reactors are required.\|[0079] e) ample opportunities to exploit waste heat streams from industry—heat may conveniently be recycled from many industries. The temperature requirements of this process fall in the medium range, at about 230° C. to 650° C. This may easily be obtained, for example, from the turbine exhaust of a gas fired power plant.\|[0080] f) lower capital costs involved at startup—The equipment used may involve commercially available reactors such as agitated tanks, filters, and columns, thereby reducing the need to invest in new technology to design new reactor types or invest in non-standard equipment before commercialization.\|[0081] g) significantly reduced energy penalty to power plant—As the main form of energy input is heat, there is no need to draw electrical energy from the power plant to drive the process. Thus, apart from some miscellaneous uses such as agitators, pumps etc, there is virtually no energy penalty to the power plant. This goes a long way towards keeping electricity costs to the consumer within acceptable ranges.\|[0082] h) applications towards diverse industries: heavy industries such as steel making, coal gasification, metal refineries and cement making emit a significant amount of CO2 in the manufacturing process. Incidentally, most of these industries involve large amounts of heating, and thus produce a lot of waste heat as well. Processes disclosed herein consume waste heat and sequesters CO2, and would be a particularly suitable candidate to partner these industries.\|[0083] Various embodiments seek to eliminate formation of ammonium chloride in the first place, thus avoiding additional regeneration steps and their associated complications altogether. As a substitute, metal chloride hydrolysis is employed as the preferred method to regenerate HCl.\|[0084] There may be four distinct stages to the process, namely: 1) acid digestion of ultramafic mineral raw material; 2) removal of impurities from the leachate solution and concurrent evaporation of water; 3) regeneration of acid for further reuse in the acid digestion step; and 4) the actual mineralization reaction to produce alkaline earth metal carbonates from carbon dioxide.\|[0085] The description of the process, from this point on, will use serpentine, which is a form of ultramafic rock material, as a representative starting mineral for illustration purposes.	(US9896741)\|TECHNICAL FIELD\|[0002] The invention relates to methods of producing metal carbonate from an ultramafic rock material.\|BACKGROUND\|[0003] Heavy industries such as steel making, coal gasification, metal refineries, power plants and cement making units emit a significant amount of carbon dioxide (CO2). Taking Singapore, for example, it was estimated that amount of carbon dioxide from power plants will exceed 20 million tonnes per year for the next decade (see TABLE 1).\|[0004] TABLE 1 Carbon dioxide (CO2) emissions from power plants in Singapore (2007-2017) 2007 Energy and CO2 Emission2017 Energy and CO2 Emission CO2Emission CO2Emission EnergyEmissionrateEnergyEmissionratePower PlantMWh/aMt CO2/at CO2/hrMWh/aMt CO2/at CO2/hr TUAS8,867,2754.0045717,100,00013.201507PULAU SERAYA8,297,8683.9344813,000,0006.00685SENOKO11,200,0004.4550811,500,0004.56520PULAU MERLIMAU0 2,931,1241.29147ISLAND POWER0 2,537,8751.27145PULAU SAKRA2,090,1030.871002,177,4970.91104SINGAPORE CHEMICAL684,5770.38431,610,5930.8395JURONG325,7140.1518363,8600.1719SINGAPORE OLEFINS318,4060.1517332,2270.1618CHANGI WWTP257,3030.1214276,9990.1315SMPO COGEN173,3210.1112182,3920.1113PASIR PANJANG185,0810.0910200,6640.1011Total32,399,64814.3 52,213,23028.7 Source: http://carma.org/region/detail/169\|[0005] Carbon dioxide capture and storage by mineralization has been proposed as a possible technology to reduce global carbon dioxide levels. The technology may include extracting cations from feed material such as rocks, and combining the cations with carbon dioxide to form a stable carbonate material. Due to the large quantities (gigatonnes) of material involved, ability to extract metal from the feed material at high efficiencies is important. Limitations to existing processes include low metal extraction yields and high energy consumption, due to removal of water which has high latent and sensible heat.\|[0006] In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|SUMMARY\|[0007] In a first aspect, a method of producing a metal carbonate from an ultramafic rock material is provided. The method comprises\| - a) providing an ultramafic rock material comprising a metal silicate;\| - b) reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| - c) contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| - d) heating the resultant mixture from step c) to decompose the salt of the metal to form metal oxide; and\| - e) reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|[0013] In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided. The system comprises\| - a) a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal;\| - b) an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture;\| - c) a furnace configured to heat the resultant mixture from step b) to decompose the salt of the metal to form the metal oxide; and\| - d) a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to form the metal carbonate.\|(US9896741)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0018] The invention will be better understood with reference to the detailed description when considered in conjunction with the non-limiting examples and the accompanying drawings, in which:\|[0019] FIG. 1 is a schematic diagram depicting working mechanism of an air stripper column. Notations in the figures represent the following: 101: packed column; 102: packing material; 103: packing support; 104: packing restrainer; 105: liquid redistributors; 106: blower assembly; 111: contaminant influent; 112: spray; 113: air in; 114: gas out to atmosphere or secondary treatment; and 115: treated effluent.\|[0020] FIG. 2 is a schematic diagram showing process flow for a mineralization process according to an embodiment.\|[0021] FIG. 3 is a graph showing thermogravimetric analysis (TGA) results of MgCl2.6H2O. Y-axis: weight; x-axis: temperature (° C.).\|[0022] FIG. 4 is a graph showing TGA analysis of magnesium carbonate product from reaction of MgO with (NH4)2CO3. Y-axis: weight (mg); x-axis: temperature (° C.).\|[0023] FIG. 5 is a schematic diagram showing general process flow for a system to carry out mineralization process according to embodiments.\|(US9896741)\|DETAILED DESCRIPTION\|[0024] Using methods disclosed herein, carbon dioxide emitted from various sources, such as coal gasification and power plants, may be captured in the form of metal carbonates such as magnesium carbonate, without significant modification of existing infrastructure. The metal carbonates are thermodynamically stable and inert, and once bound, the carbon dioxide that is captured is not susceptible to re-emission into the atmosphere. Furthermore, the metal carbonates produced may be in solid form to render their ease of handling.\|[0025] Various embodiments disclosed herein are particularly suited for long-term sequestration of carbon dioxide emitted from industries. Advantageously, systems for producing metal carbonate disclosed herein may be integrated into existing infrastructure of industries so as to utilize waste heat from the industries in production of metal carbonates. The metal carbonates produced may be used as building materials or for land reclamation purposes, or be used as additives for adding to polymers as fire retardants.\|[0026] With the above in mind, various embodiments refer in a first aspect to a method of producing a metal carbonate from an ultramafic rock material.\|[0027] The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate.\|[0028] As used herein, the term “ultramafic rock material” refers to igneous and meta-igneous rocks which are composed of more than 90% mafic minerals in various proportions with trace amounts of other minerals. The term “mafic” is used to describe a silicate mineral or rock that is rich in magnesium. Apart from magnesium, the ultramafic rock material may also contain metals such as iron, nickel, chromium, manganese and/or calcium as impurities.\|[0029] Main mafic minerals include olivine (Mg2SiO4), orthopyroxene (MgSiO3), and clinopyroxene ((MgCa)SiO3). Upon hydration, the corresponding mafic minerals are serpentine (Mg3Si2O5(OH)4), tremolite (Mg5Ca2Si8O22(OH)2), and talc (Mg3Si4O10(OH)2).\|[0030] Of particular importance is serpentine, as it is volumetrically dominant on a global scale. Typically, serpentine has a silica content of less than 45%, magnesium oxide content of greater than 18%, and a high iron oxide content in the range of about 5% to 15%. Content of serpentine may vary between the stated ranges depending on source and quality of the rock. TABLE 2 depicts composition of serpentine according to an embodiment. The values are obtained from direct measurements of the mineral samples using X-ray fluorescence spectroscopy.\|[0031] TABLE 2 Composition of Serpentine (Percentage expressed in terms of weight% of the respective oxides contained within the material)ElementMgOSiO2Fe2O3Al2O3Cr2O3CaONiOMnO Percent46.7242.78.40.610.450.40.290.14 \|[0032] In various embodiments, the ultramafic rock material comprises or consists of serpentine.\|[0033] As mentioned above, the ultramafic rock material is rich in magnesium. Accordingly, in various embodiments, the method of producing metal carbonate from an ultramafic rock material is used to produce magnesium carbonate. Molar ratio of metal to carbonate (CO3) in the metal carbonate may be in the range of about 1:1 to about 5:4. In various embodiments, molar ratio of metal to CO3 in the metal carbonate is about 1:1.\|[0034] The method includes providing an ultramafic rock material comprising a metal silicate. In various embodiments, the metal silicate is magnesium silicate, such as Mg3Si2O5(OH)4. Apart from magnesium silicate, silicates of other metals contained in the ultramafic rock material may also be present, such as silicates of iron, nickel, chromium, manganese, and/or calcium.\|[0035] Providing an ultramafic rock material comprising a metal silicate may include physically working the ultramafic rock material such as by crushing or grinding, so as to reduce size of the ultramafic rock material. Advantageously, by reducing size of the ultramafic rock material, liberation of metal from the ultramafic rock material may be accelerated.\|[0036] In some embodiments, providing an ultramafic rock material includes physically working the ultramafic rock material to form ultramafic rock particles having a size of 0.5 mm or less. Size of the ultramafic rock particles may be characterized by its maximal dimension, wherein the term “maximal dimension” refers to the maximal length of a straight line segment passing through the center of a figure and terminating at the periphery.\|[0037] For example, the ultramafic rock material may comprise or consist of ultramafic rock particles having a size of 0.5 mm or less, such as a size in the range of about 0.01 mm to about 0.5 mm, about 0.05 mm to about 0.5 mm, about 0.1 mm to about 0.5 mm, about 0.2 mm to about 0.5 mm, about 0.01 mm to about 0.3 mm, about 0.01 mm to about 0.1 mm, or about 0.1 mm to about 0.3 mm.\|[0038] The method includes reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal. In reacting the ultramafic rock material with an acid, metal from the ultramafic rock material may be leached out in the form of a metal salt. Hence, the mixture containing the salt of the metal may otherwise be termed as the leachate. A solid residue of coarse silica may also be obtained following reacting of the ultramafic rock material with acid.\|[0039] The acid may, for example, be selected from the group consisting of hydrohalic acid, sulfuric acid (H2SO4), nitric acid (HNO3), phosphoric acid (H3PO4), acetic acid (CH3COOH), and combinations thereof. Depending on the acid used, different metal salts may be formed. For example, salt of the metal may be a halide such as a chloride or a bromide, a sulfate, a nitrate, a phosphate, and/or an acetate. In various embodiments, the acid is a hydrohalic acid, such as hydrofluoric acid (HF), hydrochloric acid (HCl), hydrobromic acid (HBr), and/or hydroiodic acid (HI). In some embodiments, the acid comprises or consists of hydrochloric acid and/or hydrobromic acid.\|[0040] In specific embodiments, the acid comprises or consists of hydrochloric acid. By reacting the ultramafic rock material with hydrochloric acid, metal may be leached from the ultramafic rock material as metal chloride. Use of hydrochloric acid has been found by the inventors to be advantageous, as hydrochloric acid is able to leach metal effectively from ultramafic rock material, and may be regenerated easily and simply without complication. Undesirable decompositions do not take place upon heating of metal chlorides, as opposed to the case of metal nitrates formed from reacting metal silicates with nitric acid, for example, which may generate nitrite and nitrous products.\|[0041] The mixture may accordingly contain chlorides of magnesium, iron, nickel, chromium, manganese, and/or calcium. Due to the high magnesium content in ultramafic rock material, the salt of the metal may mainly be made up of magnesium chloride.\|[0042] In various embodiments, concentration of the hydrochloric acid is at least 27 wt % HCl. For example, concentration of the hydrochloric acid may be at least 30 wt %, at least 35 wt % HCl, or be in the range of about 27 wt % to about 35 wt %, about 27 wt % to about 32 wt %, or about 27 wt % to about 30 wt % HCl.\|[0043] Reacting the ultramafic rock material with an acid may be carried out at a temperature in the range of about 80° C. to about 100° C. For example, reacting the ultramafic rock material with an acid may be carried out at a temperature in the range of about 80° C. to about 95° C., about 80° C. to about 90° C., about 80° C. to about 85° C., about 90° C. to about 100° C., or about 85° C. to about 95° C. In various embodiments, reacting the ultramafic rock material with an acid is carried out under continuous stirring to accelerate liberation of metal from the ultramafic rock material.\|[0044] The method includes contacting the mixture comprising a salt from the metal with oxygen. The oxygen may be in the form of an oxygen flow and/or an air flow. This may be carried out to aerate impurities in the mixture and/or to remove residual acid from the mixture. As mentioned above, the ultramafic rock material may also contain metals such as iron, nickel, chromium, manganese and/or calcium as impurities. By contacting the mixture comprising a salt of the metal with oxygen, the metals may be aerated to their respective oxides and may be precipitated out from the mixture to allow their removal from the resultant mixture by a separation process such as decanting or filtering.\|[0045] By way of example only, this aeration process may be illustrated using hydrochloric acid and iron. Iron may be leached from ultramafic rock material using hydrochloric acid to form iron (II) chloride (FeCl2). The iron (II) chloride may be oxidized readily to iron (III) chloride (FeCl3) upon contact with oxygen, as shown in equation (1):\|12FeCl2+3O2→2Fe2O3+8FeCl3 (1)\|[0046] The iron (III) chloride may undergo auto-hydrolysis in solution to form iron (III) oxide and hydrogen chloride, as shown in equation (2):\|2FeCl3+3H2O→Fe2O3+6HCl (2)\|[0047] Iron (III) oxide may be precipitated out from the mixture following oxidation to allow their easy removal.\|[0048] In various embodiments, contacting the mixture comprising a salt of the metal with oxygen to aerate impurities in the mixture comprises separating oxides of iron, nickel, chromium, aluminum and/or manganese from the resultant mixture following oxidation.\|[0049] Further, from equation (2), it may be seen that by eliminating hydrochloric acid from the solution, conversion of iron (III) chloride into iron (III) oxide may be promoted. This means that metal impurities in the mixture may be removed to a greater extent by removing hydrochloric acid from the mixture. Advantageously, the removal of hydrochloric acid, which may arise from the auto-hydrolysis process as well as residual acid present in the mixture, may be carried out by contacting the mixture comprising a salt of the metal with oxygen.\|[0050] Contacting the mixture comprising a salt of the metal with oxygen may be carried out in a flow of air and/or oxygen. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out by air stripping. As used herein, the term “air stripping” refers to a process by which an air stream is used to remove dissolved gases or volatile components of a liquid. The air stripping may be carried out in an air stripper column. For example, the mixture comprising a salt of the metal may be introduced at the top of an air stripper column. The air stripper column may contain packing material to provide a larger contact surface area for aeration. Air may be introduced at the bottom of the air stripper column, such that the mixture flows in opposite direction to the ascending air while contacting each other. In so doing, the air may strip acid from the mixture. The air exits from the top of the air stripper column, while the resultant mixture, which has been at least partially stripped of acid, may leave the bottom of the air stripper column for channeling into a subsequent stage.\|[0051] In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out under conditions such that pH of the mixture is less than or equal to 9. For example, the contacting may be carried out under conditions such that pH of the mixture is in the range of about 3 to about 9, about 5 to about 9, about 7 to about 9, about 3 to about 7, about 3 to about 5, about 5 to about 7, or about 4 to about 6.\|[0052] Contacting the mixture comprising a salt of the metal with oxygen may be carried out at a temperature in the range of about 150° C. to about 250° C., such as about 180° C. to about 250° C., about 200° C. to about 250° C., about 150° C. to about 220° C., about 150° C. to about 200° C., about 180° C. to about 220° C., or about 180° C. to about 200° C. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature in the range of about 180° C. to about 200° C. In some embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out at a temperature of about 200° C.\|[0053] By contacting the mixture comprising a salt of the metal with oxygen at elevated temperatures, water may be evaporated or vaporized from the mixture to form steam. In various embodiments, contacting the mixture comprising a salt of the metal with oxygen is carried out for a time period suitable to form a mixture saturated with the salt. Advantageously, by removing water from the mixture, this minimizes water content in the mixture for removal in a subsequent stage. At the same time, heat energy may be recovered in the form of steam for rechanneling back into the process.\|[0054] By removing water from the mixture, a hydrated salt of the metal may also be formed. In various embodiments, the hydrated salt of the metal comprises or consists essentially of magnesium chloride hydrates. Water of crystallization of the hydrated metal salt may be in the range of about 2 to about 6, such as 2, 3, 4, 5, or 6.\|[0055] The method of the first aspect includes heating the resultant mixture following contact with oxygen to decompose the salt of the metal to form metal oxide. For example, the metal oxide may contain magnesium oxide, along with trace amounts of oxides of iron, nickel, chromium, manganese, and/or calcium which may not have been removed in an earlier stage.\|[0056] In various embodiments, heating the resultant mixture is carried out at a temperature in the range of about 400° C. to about 600° C., such as about 450° C. to about 600° C., about 500° C. to about 600° C., about 550° C. to about 600° C., about 400° C. to about 550° C., or about 450° C. to about 550° C. In specific embodiments, heating the resultant mixture is carried out at a temperature of about 550° C.\|[0057] Given the high temperatures, steam may be generated. In embodiments where the acid is hydrochloric acid, and where residual acid is present in the resultant mixture not removed in an earlier stage, hydrogen chloride gas may additionally be produced.\|[0058] The metal oxide is reacted with aqueous ammonium carbonate to obtain the metal carbonate. At the same time, aqueous ammonia may be produced.\|[0059] The aqueous ammonium carbonate may be obtained by reacting carbon dioxide with aqueous ammonia, which may be carried out in a gas-liquid packed column. The carbon dioxide may be comprised in a flue gas, which may be channeled from heavy industries such as a power plant.\|[0060] Molar ratio of aqueous ammonia to carbon dioxide may be in the range of about 2:1 to about 2.5:1, such as about 2.1:1, 2.2:1, 2.3:1, 2,4:1, or about 2.5:1.\|[0061] In various embodiments, reacting carbon dioxide with aqueous ammonia is carried out at a pH of at least 9 to maximize degree of carbonation. For example, reacting carbon dioxide with aqueous ammonia may be carried out at a pH in the range of about 9 to about 13, about 9 to about 12, about 9 to about 11, about 9 to about 10, about 10 to about 13, about 11 to about 13, or about 10 to about 12. In some embodiments, reacting carbon dioxide with aqueous ammonia is carried out at a pH of at least 10.\|[0062] Advantageously, reacting the metal oxide with aqueous ammonium carbonate may be carried out at ambient conditions.\|[0063] In a second aspect, a system for producing a metal carbonate from ultramafic rock material is provided. The system comprises a reactor configured to carry out reaction of an ultramafic rock material with an acid to form a mixture comprising a salt of the metal; an air stripper column configured to contact the mixture comprising a salt of the metal with oxygen to aerate impurities in the mixture and/or to remove residual acid from the mixture; a furnace configured to heat the resultant mixture to decompose the salt of the metal to form the metal oxide; and a precipitator configured to carry out reaction of the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. Schematic diagram of a system for producing a metal carbonate from ultramafic rock material according to embodiments is shown in FIG. 5 and discussed in Example 8. Processing conditions for operating the various components of the system have already been discussed above.\|[0064] In various embodiments, the system further comprises a gas-liquid packed column arranged upstream of the precipitator and configured to carry out reaction of carbon dioxide with aqueous ammonia to form aqueous ammonium carbonate. As mentioned above, the carbon dioxide may be comprised in a flue gas, which may be channeled from heavy industries such as a power plant. The ammonium carbonate that is formed may be used to react with the metal oxide to form metal carbonate. In so doing, carbon dioxide may be captured in the metal carbonate which is thermodynamically stable and inert, thereby rendering the carbon dioxide that is captured not susceptible for re-emission into the atmosphere.\|[0065] The system may further comprise a compressor configured to compress acid vapor and/or water vapor from the air stripper column. This allows formation of higher quality steam that may be used to supplement heating medium that may be used for operating the air stripper column.\|[0066] The system may, in various embodiments, comprise recycling means configured to recycle acid vapor and/or water vapor from the air stripper column and/or the furnace to the reactor and/or the air stripper column. In so doing, heat energy that is generated from the air stripper column and/or the furnace may be reused in other parts of the process, thereby minimizing energy consumption of the system.\|[0067] In various embodiments, the system further comprises recycling means configured to recycle aqueous ammonia from the precipitator to the gas-liquid packed column. As mentioned above, metal oxide may be reacted with aqueous ammonium carbonate to obtain metal carbonate in the precipitator, while producing aqueous ammonia at the same time. By recycling the aqueous ammonia produced to the gas-liquid packed column, the aqueous ammonia may be reused to react with carbon dioxide to form aqueous ammonium carbonate.\|[0068] Hereinafter, the present invention will be described more fully with reference to the accompanying drawings, in which exemplary embodiments of the invention are shown. This invention may, however, be embodied in many different forms and should not be construed as limited to the exemplary embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art. In the drawings, lengths and sizes of layers and regions may be exaggerated for clarity.\|[0069] As used herein, the term “and/or” includes any and all combinations of one or more of the associated listed items. The invention illustratively described herein may suitably be practiced in the absence of any element or elements, limitation or limitations, not specifically disclosed herein. Thus, for example, the terms “comprising”, “including”, “containing”, etc. shall be read expansively and without limitation. Additionally, the terms and expressions employed herein have been used as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the invention claimed. Thus, it should be understood that although the present invention has been specifically disclosed by preferred embodiments and optional features, modification and variation of the inventions embodied therein herein disclosed may be resorted to by those skilled in the art, and that such modifications and variations are considered to be within the scope of this invention.\|[0070] The invention has been described broadly and generically herein. Each of the narrower species and subgeneric groupings falling within the generic disclosure also form part of the invention. This includes the generic description of the invention with a proviso or negative limitation removing any subject matter from the genus, regardless of whether or not the excised material is specifically recited herein.\|[0071] Other embodiments are within the following claims and non-limiting examples. In addition, where features or aspects of the invention are described in terms of Markush groups, those skilled in the art will recognize that the invention is also thereby described in terms of any individual member or subgroup of members of the Markush group.\|EXPERIMENTAL SECTION\|[0072] Various embodiments described herein relate to a process to convert gaseous carbon dioxide from flue gas into a mineralized form, bound to alkaline earth metals obtained from ultramafic rocks. A general overall equation, employing serpentine (Mg3Si2O5(OH)4) as a representative starting material, to describe the process is as follows:\|Mg3Si2O5(OH)4+3CO2→3MgCO3+2SiO2+2H2O\|[0073] The carbon dioxide is converted into a carbonate, which is thermodynamically more stable and inert. The solid form of the carbonate is easily handled and once bound, the carbon dioxide is not susceptible to re-emission into the atmosphere unless subjected to extreme conditions.\|[0074] Improvements over state-of-the-art mineralization routes include:\|[0075] a) lower energy consumption—It is readily apparent that the net CO2 capture amount for the process described herein is positive, at least in cases where natural gas and oil are the preferred fossil fuels for combustion. This cannot be said for state of the art mineralization processes. The utilization of direct thermal energy significantly contributes to much lower CO2 emissions per ton CO2 captured. In the case of Singapore, which utilizes natural gas as the preferred fuel of choice for power generation, every 2,500 kWh produces one ton of CO2. The amount of CO2 avoided in this case is around 30%, if other assorted electrical energy uses (such as for agitation, milling, and pumping) are taken into account.\|[0076] b) established fundamentals of reactions—kinetics and thermodynamics of decomposition, as well as processes of producing anhydrous MgCl2 have been studied as MgCl2 is an important precursor to electrolytic production of magnesium metal, and thus is of strategic importance.\|[0077] c) avoidance of messy and uncontrollable side reactions—one distinct advantage of using an HCl as a leaching medium is that the regeneration reaction to yield acid is relatively uncomplicated. There are no unwanted secondary decompositions when heating is applied, unlike when nitrates are involved (there is a possibility of nitrite and nitrous products forming when pyrolysis of the nitrate salt occurs).\|[0078] d) relatively small reactor sizes—the scale of operations, when it comes to carbon capture, often involves millions of tons of material being conveyed and pumped annually. Thus, it is desirable to use concentrated solutions or gases in order to reduce infrastructure and operating costs. In fact, one may even argue that a more concentrated solution facilitates certain steps in the process, such as the evaporation stages. Since magnesium chloride is highly soluble in water, a very concentrated leachate solution may be obtained, and thus only relatively small reactors are required.\|[0079] e) ample opportunities to exploit waste heat streams from industry—heat may conveniently be recycled from many industries. The temperature requirements of this process fall in the medium range, at about 230° C. to 650° C. This may easily be obtained, for example, from the turbine exhaust of a gas fired power plant.\|[0080] f) lower capital costs involved at startup—The equipment used may involve commercially available reactors such as agitated tanks, filters, and columns, thereby reducing the need to invest in new technology to design new reactor types or invest in non-standard equipment before commercialization.\|[0081] g) significantly reduced energy penalty to power plant—As the main form of energy input is heat, there is no need to draw electrical energy from the power plant to drive the process. Thus, apart from some miscellaneous uses such as agitators, pumps etc, there is virtually no energy penalty to the power plant. This goes a long way towards keeping electricity costs to the consumer within acceptable ranges.\|[0082] h) applications towards diverse industries: heavy industries such as steel making, coal gasification, metal refineries and cement making emit a significant amount of CO2 in the manufacturing process. Incidentally, most of these industries involve large amounts of heating, and thus produce a lot of waste heat as well. Processes disclosed herein consume waste heat and sequesters CO2, and would be a particularly suitable candidate to partner these industries.\|[0083] Various embodiments seek to eliminate formation of ammonium chloride in the first place, thus avoiding additional regeneration steps and their associated complications altogether. As a substitute, metal chloride hydrolysis is employed as the preferred method to regenerate HCl.\|[0084] There may be four distinct stages to the process, namely: 1) acid digestion of ultramafic mineral raw material; 2) removal of impurities from the leachate solution and concurrent evaporation of water; 3) regeneration of acid for further reuse in the acid digestion step; and 4) the actual mineralization reaction to produce alkaline earth metal carbonates from carbon dioxide.\|[0085] The description of the process, from this point on, will use serpentine, which is a form of ultramafic rock material, as a representative starting mineral for illustration purposes.\|(US9896741)\|Example 1: Acid Digestion of Ultramafic Mineral Raw Material and Purification of Leachate\|[0086] Serpentine, ground to particles with sizes of 0.5 mm or less, was reacted with an acid, preferably hydrochloric acid (HCl) to leach out the magnesium contained therein:\|Mg3Si2O5(OH)4(s)+6HCl(aq)→3 MgCl2(aq)+2SiO2(s)+5H2O (1)\|[0087] This extraction step is conducted at 80° C. to 100° C. in a continuously stirred tank reactor (CSTR).\|[0088] The selection of acid used is of great importance, as it affects the reactor sizes and regeneration steps, as can be seen from descriptions later in the text. At least five types of commonly available acids (HCl, H2SO4, HNO3, H3PO4 and CH3COOH) were considered for the leaching step. Of the acids considered, HCl fulfils both the requirements of effective leaching and complication-free regeneration.\|[0089] Magnesium salts of SO42− and PO43− were poorly soluble, necessitating larger reactors to accommodate the more dilute solution produced. Magnesium acetate was reasonably soluble, but the leaching rate was unsatisfactory due to acetic acid being a weak acid. Only Mg(NO3)2 offered comparable solution concentrations and leaching rates to MgCl2. The kinetics of decomposition of Mg(NO3)2, however, is considerably more complicated and less well defined, as it involves the uncontrolled formation of numerous nitrogen species.\|Example 2: Removal of Impurities from Leachate Solution and Concurrent Evaporation of Excess Water\|[0090] Iron, nickel, chrome, manganese and calcium also exist in serpentine ore as impurities such as that shown in TABLE 2. Since it is nearly impossible to inhibit the co-extraction of these elements during the acid leaching step, it is necessary to remove them in a separate step to separate Fe, Ni, Mn and Cr oxides, which are high value added metal salts, to ensure that high purity magnesite is obtained at the end of the process. To this extent, the leachate solution is first filtered to remove the remaining silica. Next, iron dissolved in the leachate solution is precipitated either as hematite or any of its hydrated forms.\|[0091] To accomplish this, the iron-containing leachate is passed through a heated air stripper to aerate the leachate solution and to flush off any remaining unreacted HCl that is dissolved in solution. Dissolved HCl is removed from the solution via contact with supplied air from the bottom of the stripper column, FIG. 1 describes the mechanisms of an air stripper column.\|[0092] The rationale behind this stripping step is based on the facts that 1) ferrous chloride may be readily oxidized to ferric chloride via contact with oxygen:\|12FeCl2+3O2→2Fe2O3+8FeCl3 \|[0093] and 2) iron chlorides in solution may undergo auto-hydrolysis to form iron oxides and hydrogen chloride:\|2FeCl3+3H2O→Fe2O3+6HCl\|[0094] When combined, both reactions may result in the near-total conversion of iron chlorides into iron oxide solids.\|[0095] Degree of auto-hydrolysis is governed by the following equation:\|[0096] \|[0097] Thus, it may be seen that by eliminating HCl from the solution, conversion of FeCl3 into iron oxides may be promoted which may be conveniently filtered from the leachate solution. After removing the iron content, the filtrate is essentially a near saturated MgCl2 solution. It should be noted that the iron oxidation and hydrolysis steps are ideally conducted at 200° C.\|[0098] Apart from stripping HCl from the leachate solution, excess water may also be evaporated to yield magnesium chloride hexahydrate. It is important for concentration of the solution to be as high as possible, as this minimizes the amount of water that needs to be evaporated in a subsequent stage. A saturated leachate solution (circa 5 M of MgCl2, or about 33 wt %) is ideal for operation purposes. In the case of a 33 wt % leachate solution, 5.11 mols of free water would have to be evaporated to yield 1 mol of MgCl2.6H2O. The required heat for this evaporation is:\|5.11H2O(l)→5.11H2O(g) Tmin=100° C., ΔH=208 kJ/mol\|[0099] At 200° C., the hexahydrate salt also undergoes partial dehydration to produce a tetrahydrate salt, shown in the following equation:\|MgCl2.6H2O(s/l)→MgCl2.4H2O(s/l)+2H2O(g) Tmin=100° C., ΔH=116 kJ/mol\|[0100] The total heat required to allow these transformations to occur was thus estimated to be at 323 kJ/mol MgCl2.\|[0101] The steam evolved from evaporation of excess water in this step may be recompressed in a mechanical vapor recompressor, resulting in higher quality steam that may be used to supplement the heating medium that is required for this step.\|[0102] Scaling due to salt precipitation may be avoided, as at temperatures above 117° C., the hydrated salt melts into a molten salt hydrate (MSH). This molten MgCl2 solution may then be transferred to the acid regeneration stage.\|Example 3: Regeneration of Acid Solution\|[0103] The molten salt hydrate may be decomposed into MgO and HCl, according to the following reactions (see Example 5 below for more information):\|MgCl2.4H2O(s/l)→MgCl2.2H2O(s/l)+2H2O(g) Tmin=134° C., ΔH=134 kJ/mol\|MgCl2.2H2O(s/l)→MgOHCl(s)+HCl(g)+H2O(g) Tmin=218° C., ΔH=141 kJ/mol\|MgOHCl(s)→MgO(s)+HCl(g) Tmin=550° C., ΔH=98 kJ/mol\|[0104] The hydrated salt may first be dehydrated, and then undergoes hydrolysis in the presence of water to give hydrogen chloride gas and magnesium oxide. The overall reaction for decomposing MgCl2.4H2O may thus be:\|MgCl2.4H2O(s)→MgO(s)+2HCl(g)+3H2O(g) T=550° C., ΔH=373 kJ/mol\|[0105] An enormous amount of heat may be carried away from the furnace in the form of water vapour and HCl gas. According to the decomposition reaction formula, 3 mols of water vapour are formed for every mol of MgO produced, as well as 2 mols of HCl gas that when dissolved into water, yields 75 kJ/mol of dissolution heat. This heat may be reused in other parts of the process, most notably the impurity removal and evaporation step. It should be noted that the heat required by the evaporator may be less than the heat carried off by the decomposition products from the furnace.\|[0106] As can be seen from the above, it is possible to recycle waste heat from the furnace to be used in the evaporation step, provided that the following three conditions are met: 1) the leachate solution is sufficiently concentrated (not less than 28 wt % MgCl2); 2) the leachate stream enters the evaporator at not less than 100° C. and 3) proper insulation is applied such that heat losses are not significant.\|[0107] The formed MgO solids at the end of the HCl regeneration step may then be transferred to the CO2 mineralization stage, and the HCl may be reused in the acid leaching reaction.\|Example 4: Mineralization of Carbon Dioxide\|[0108] MgO obtained from the end of the previous stage may be contacted with aqueous ammonium carbonate ((NH4)2CO3) from a CO2 scrubbing process to produce solid magnesium carbonate and aqueous ammonia (see Example 7 below for more information). The solid magnesium carbonate may be filtered off, yielding an ammonia solution that may be reused for CO2 removal. The reaction for CO2 removal from flue gas, via ammonia capture, is shown below (see Example 6 below for more information):\|2NH3(aq)+CO2(g)+H2O(l)→(NH4)2CO3(aq)\|[0109] The CO2 removal may be conducted in a packed scrubbing tower, in order to maximize the contacting surface area of the ammonia solution with CO2 gas. The operating conditions and ratio of NH3 to CO2 should be controlled to stay within an optimal range, to avoid formation of by-products such as ammonium bicarbonate (NH4HCO3) and urea ((NH2)2CO). The recommended molar ratio of NH3 to CO2 is about 2:1 to about 2.5:1.\|[0110] Estimations based on HSC software indicate that the reaction between MgO and aqueous (NH4)2CO3 may be favorable at ambient temperatures and pressures, and is exothermic:\|[0111] TABLE 3 Simulation results from HSC for the reaction between MgO and (NH4)2CO3MgO + (NH4)2CO3(ia) = MgCO3(M) + 2NH3(a) + H2O(l)T (° C.)ΔH (kJ)ΔS (J/K)ΔG (kJ)KLog(K) 0.000−21.872135.220−58.8081.765E+01111.24710.000−19.546143.582−60.2011.278E+01111.10720.000−17.009152.387−61.6819.805E+01010.99130.000−14.338161.344−63.2497.929E+01010.89940.000−11.571170.323−64.9086.726E+01010.82850.000−8.732179.246−66.6565.960E+01010.77560.000−5.836188.071−68.4925.493E+01010.74070.000−2.893196.777−70.4175.246E+01010.72080.0000.093205.353−72.4275.173E+01010.71490.0003.118213.798−74.5235.250E+01010.720100.0006.179222.114−76.7035.470E+01010.738 \|[0112] In conclusion, the entire process may be depicted by FIG. 2.\|Example 5: Hydrolysis of Magnesium Chloride Hexahydrate to Magnesium Oxide\|[0113] Hydrolysis of MgCl2.6H2O was studied via thermogravimetric analysis (TGA). Results are shown in FIG. 3.\|[0114] As may be seen from the figure, the hexahydrate salt was dehydrated at temperatures up to 120° C., losing four moles of water per mole of MgCl2.6H2O. The resulting dihydrate salt underwent a first hydrolysis, liberating one mole of water and one mole of HCl to yield MgOHCl. The first hydrolysis was completed at around 220° C.\|[0115] When further heated to 400° C., the hydroxychloride underwent a second hydrolysis, generating another mole of HCl and leaving behind a solid MgO residue.\|Example 6: Reaction of Carbon Dioxide with Aqueous Ammonia\|[0116] An experiment was conducted to demonstrate feasibility of aqueous ammonia as a sorbent for CO2.\|[0117] 0.5 L of 6 M aqueous ammonia solution was prepared by diluting 0.225 L of stock aqueous ammonia (25 wt %) with 0.275 L deionized (DI) water. The solution was immersed in an ice bath and sparged with carbon dioxide gas (3 bar outlet pressure). The pH and temperature in relation to time was recorded in TABLE 4 below.\|[0118] TABLE 4 Time, pH and temperature of aqueous ammonia solutionTime (h)pHTemperature (° C.) 013120.5127111.614211.318310.984410.754510.584 \|[0119] It may be seen that aqueous ammonia may effectively absorb CO2 under the right conditions. Note that the mass transfer and absorption rates may be significantly improved by using a suitably designed scrubber or gas/liquid contactor.\|Example 7: Reaction of Magnesium Oxide with Ammonium Carbonate\|[0120] 14.4 grams (0.15 mols) of ammonium carbonate was dissolved in 150 ml DI water to produce a 1 M ammonium carbonate solution. 4 grams (0.1 mols) of magnesium oxide was added to this solution and stirred for 1 hour at ambient temperature and pressure. Warming of the solution occurred for the first half hour, suggesting that a carbonation reaction was taking place. After thirty minutes, an apparent cooling of the slurry to room temperature was observed.\|[0121] The solids were filtered from the solution and dried in an oven overnight at 80° C. The dried solids were studied using thermogravimetric analysis (TGA) to determine the degree of carbonation. The results are shown in FIG. 4.\|[0122] The results from the figure show that the sample underwent a slow dehydration at temperatures up to 250° C., and loss of CO2 at temperatures above 400° C.\|[0123] Calculations from the data also indicated a H2O:CO2:MgO ratio of 0.87:0.85:1, suggesting a species similar in composition to hydromagnesite (Mg5(CO3)4(OH)2.4H2O).\|Example 8: Exemplary Embodiment of a System\|[0124] FIG. 5 is a schematic diagram showing general process flow for a system to carry out mineralization process according to embodiments.\|[0125] An aqueous leaching process involving HCl and alkaline-earth silicate minerals may take place in R1. The leaching process in R1 may involve reacting aqueous HCl solution with alkaline-earth silicate minerals at not less than 27 wt % HCl and 80° C. to extract the alkaline-earth elements into a leachate solution from the minerals.\|[0126] The leachate solution (Si) from R1 may be subjected to purification by stripping unreacted HCl from the leachate to precipitate impurities from the liquid phase, which may take place in R2.\|[0127] Removal of impurities in R2 may be aided by oxidation of any intermediate species, for example from ferrous to ferric iron, such that they are more easily removed. The oxidation step in R2 may be conducted by introduction of air or oxygen into the leachate solution.\|[0128] Stripping of HCl in R2 may be controlled such that the pH of the leachate solution goes up to, but does not exceed 9. Stripping of HCl in R2 may be conducted in a temperature range of 150° C. to 250° C., more preferably 180° C. to 200° C. The purified leachate solution from R2 may be subjected to evaporation to produce MgCl2 hydrates, where the water of crystallization is between the numbers of 2 to 6.\|[0129] The above-mentioned chemical transformations may be conducted in a single reactor R2, which may be a heated air stripper. The heated air stripper R2 may be maintained at a temperature not less than 180° C., preferably at 200° C. or more. The evaporated water (S4) from R2 may be recycled to the leaching process in R1. The produced MgCl2 hydrates (S2) from R2 may be subjected to thermal hydrolysis in a furnace R3 to yield MgO (S5), HCl and water vapor. The HCl and water vapor from R3 (S3) may be used as a heating medium for the heated air stripper R2. The HCl and water from R2 (S4) may be recycled to the leaching process in R1.\|[0130] A mechanical vapor recompressing mechanism may be used to compress exiting HCl and water vapor S4 from the heated air stripper R2. The recompressed HCl and water vapor (S4-1) may be used to supplement the heating medium.\|[0131] The aqueous (NH4)2CO3 solution (S6) may be obtained by reacting aqueous NH3 solution with CO2 in flue gas from a CO2 point source, such as a power plant.\|[0132] The CO2 capture reaction in R4 may be conducted in a gas-liquid contacting tower with sufficient packing. The carbonation reaction may be reacted at pH not less than 9, and preferably above 10, to maximize the degree of carbonation.\|[0133] The resulting aqueous NH3 solution from R5 (S7) may be recycled to the scrubbing process in R4.\|[0134] Various embodiments described herein is suitable for mitigation of CO2 emissions from all kinds of industrial sectors, such as power plants, cement plants, and steel plants, without significant modification of existing infrastructure. At the same time, the products may be used as building materials or additives to polymers as fire retardants. Particularly, various embodiments disclosed herein are suitable for long-term sequestration of CO2 emitted from local power plants and the carbonation products, carbonates and sand are utilized for land reclamation purposes in Singapore.\|[0135] The predicted amount of CO2 from local power plants for the next decade (see TABLE 1) exceeds approximately 20 million tonnes per year, which may produce about 60 million tonnes or 25 million m3/a of carbonate and sand by this CO2 sequestration process. On an average scale, the landfill area is projected to expand by 1 km2 per year for the next 10 years. Therefore, various embodiments disclosed herein for application to mineral carbonation process is viewed as a promising approach which provides environmental benefits particularly for Singapore.\|[0136] While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it will be understood by those of ordinary skill in the art that various changes in form and details may be made therein without departing from the spirit and scope of the present invention as defined by the following claims.	Family Number\|(69805816)\|69805816\|Abstract\|(WO201599612 A1)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.\|(AU2014370454 B2)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.\|(SG11201605164Y B)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.(From US9896741 B2)\|(US9896741 B2)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.\|Advantages / Prev. Drawbacks\|(WO201599612 A1)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above- mentioned problems.\|(AU2014370454 B2)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the abovementioned problems.\|(AU2014370454 A1)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the abovementioned problems.\|(US9896741 B2)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|(US20160319395 A1)\|In view of the above, there exists a need for improved methods of producing metal carbonate from an ultramafic rock material, thereby capturing carbon dioxide from the atmosphere or environment, which overcome or at least alleviate one or more of the above-mentioned problems.\|	Environmental technology\|Materials, 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SELF=N	WO201088738\|US4798717\|WO201088738\|US4798717\|US4798717\|US3785797	WO201088738 1878278 WHO=Examiner SELF=N CAT=A\|US4798717 42628151 WHO=Examiner SELF=N CAT=A\|WO201088738 1878278 WHO=Applicant SELF=N\|US4798717 42628151 WHO=Applicant SELF=N\|US4798717 42628151 WHO=Examiner SELF=N\|US3785797 42106785 WHO=Examiner SELF=N		US4798717; WO201088738\|US4798717\|US3785797; US4798717; WO201088738\|	(US9896741)\|Applicant references\|-International Preliminary Report on Patentability for International Application No. PCT/SG2014/000613 dated Jun. 28, 2016, pp. 1-5.\|-Written Opinion for International Application No. PCT/SG2014/000613 dated Mar. 16, 2015, pp. 1-4.\|\|\|\|	GRANTED	(US9896741)\|GRANTED\|(WO2015/099612)\|LAPSED\|(AU2014370454)\|GRANTED\|(SG11201605164Y)\|GRANTED	ALIVE	(US9896741)\|ALIVE\|(WO2015/099612)\|DEAD\|(AU2014370454)\|ALIVE\|(SG11201605164Y)\|ALIVE	(US9896741)\|LEGAL DETAILS FOR US9896741\|Actual or expected expiration date=2035-01-20\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2014-12-23\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US15107870\|Application date=2014-12-23\|Standardized application number=2014US-15107870\|Event publication date=2014-12-23\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:BERNS, DANIEL J\|Event publication date=2014-12-23\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2014-12-23\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 40940-P085WOUS\|Event publication date=2014-12-23\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 185095\|Event publication date=2014-12-23\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular 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state=DEAD\|Status=LAPSED\|Event publication date=2014-12-23\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOSG2014/000613\|Application date=2014-12-23\|Standardized application number=2014WO-SG00613\|Event publication date=2015-07-02\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2015/099612\|Publication stage code=A1\|Publication date=2015-07-02\|Standardized publication number=WO201599612\|Event publication date=2017-06-24\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2014370454\|Actual or expected expiration date=2034-12-23\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2014370454\|Application date in the designated or member state=2014-12-23\|Application number in the 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COUNTRY=SG	\|(WO2015/099612)\|SG\|(AU2014370454)\|AU\|(AU2014370454)\|AU\|(SG11201605164Y)\|SG\|(SG11201605164Y)\|SG	(US9896741)\|NAME=Winstead, P.C.\|(WO2015/099612)\|NAME=VIERING, JENTSCHURA & PARTNER LLP P.O. Box 1088 Rochor Road Rochor Post Office Singapore 911833 , COUNTRY=SG\|(AU2014370454)\|NAME=Phillips Ormonde Fitzpatrick PO Box 323 , CITY=Collins Street West , STATE=VIC , POSTCODE=8007 , COUNTRY=AU\|(AU2014370454)\|NAME=Phillips Ormonde Fitzpatrick PO Box 323 , CITY=Collins Street West , STATE=VIC , POSTCODE=8007 , COUNTRY=AU\|(SG11201605164Y)\|NAME=VIERING, JENTSCHURA & PARTNER LLP P.O. BOX 1088<br/>ROCHOR POST OFFICE<br/>Singapore 911833 , COUNTRY=SG , REG=T06LL1666B\|(SG11201605164Y)\|NAME=VIERING, JENTSCHURA & PARTNER LLP P.O. BOX 1088<br/>ROCHOR POST OFFICE<br/>Singapore 911833 , COUNTRY=SG , REG=T06LL1666B	(US9896741)\|SG; SG; SG\|(US20160319395)\|SG; SG; SG\|(WO2015/099612)\|SG; SG; SG\|\|\|(SG11201605164Y)\|SG; SG; SG\|(SG11201605164Y)\|SG; SG; SG	(US9896741)\|NAME=Bu Jie, CITY=Singapore, COUNTRY=SG \|NAME=Yeo Tze Yuen, CITY=Singapore, COUNTRY=SG \|NAME=Sharratt Paul, CITY=Singapore, COUNTRY=SG\|(US20160319395)\|NAME=Bu Jie, CITY=Singapore, COUNTRY=SG \|NAME=Yeo Tze Yuen, CITY=Singapore, COUNTRY=SG \|NAME=Sharratt Paul, CITY=Singapore, COUNTRY=SG\|(WO2015/099612)\|NAME=BU, Jie c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=YEO, Tze Yuen c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=SHARRATT, Paul c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG\|(AU2014370454)\|NAME=Bu, Jie\|NAME=Yeo, Tze Yuen\|NAME=Sharratt, Paul\|(AU2014370454)\|NAME=Bu, Jie\|NAME=Yeo, Tze Yuen\|NAME=Sharratt, Paul\|(SG11201605164Y)\|NAME=BU, Jie c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=SHARRATT, Paul c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=YEO, Tze Yuen c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG\|(SG11201605164Y)\|NAME=BU, Jie c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=SHARRATT, Paul c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG \|NAME=YEO, Tze Yuen c/o Institute of Chemical and Engineering Sciences 1 Pesek Road Jurong Island Singapore 627833, COUNTRY=SG	(WO2015/099612)\|5\|(AU2014370454)\|5\|(US9896741)\|5	3	4			(US9896741)\|WO2015/099612\|(AU2014370454)\|WO2015/099612\|(SG11201605164Y)\|WO2015/099612		(US9896741)\|Number of Claims: NCL=20\|Number of Drawings: NDR=5\|Number of Figures: NFG=5\|Independent Claim Number: ICL=1,16\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=28\|Primary examiner: Berns Daniel\|Art Unit.: ART =1736\|\|(US20160319395)\|Number of Claims: NCL=20\|Number of Drawings: NDR=5\|Number of Figures: NFG=5\|Independent Claim Number: ICL=1,16\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: Berns Daniel\|Art Unit.: ART =1736\|\|(WO2015/099612)\|Number of Claims: NCL=20\|Extended kind: EXTK=x\|\|(AU2014370454)\|Number of Claims: NCL=20\|\|(AU2014370454)\|Number of Claims: NCL=20\|\|(SG11201605164Y)\|Number of Claims: NCL=20\|Number of Pages: NPAGES=34\|\|(SG11201605164Y)\|Number of Claims: NCL=17\|	(US9896741)\|Previous publication: US20160319395 A1 2016-11-03 [US20160319395]	(US9896741)\|ENGLISH (ENG)	(AU2014370454)\|Patent\|(US9896741)\|Patent\|(US20160319395)\|Patent\|(SG11201605164Y)\|Patent\|(AU2014370454)\|Patent\|(SG11201605164Y)\|Patent\|(WO201599612)\|Patent	Titre: (US9896741)\|Method of producing metal carbonate from an ultramafic rock material Résumé: (US9896741)\|A method of producing a metal carbonate from an ultramafic rock material is provided. The method includes providing an ultramafic rock material comprising a metal silicate; reacting the ultramafic rock material with an acid to form a mixture comprising a salt of the metal; contacting the mixture comprising a salt of the metal with oxygen so as to aerate impurities in the mixture and/or to remove residual acid from the mixture; heating the resultant mixture to decompose the salt of the metal to form metal oxide; and reacting the metal oxide with aqueous ammonium carbonate to obtain the metal carbonate. A system for producing a metal carbonate from ultramafic rock material is also provided.	30	Abstract	gpt-4o-mini	no	The focus is on producing metal carbonates from ultramafic rock materials using acid and ammonium carbonate, rather than on accelerating weathering processes for CO₂ capture.
33	US63/641,910P\|US63/716,029P\|US19/092,576	WOUS2025/022798\|US19/092,576	US20250339810\|WO2025/230667	116490379	WO2025/230667 A1 2025-11-06 [WO2025230667]\|US20250339810 A1 2025-11-06 [US20250339810]	2024-05-02\|2024-11-04\|2025-03-27	2025-04-02\|2025-03-27	2025-11-06\|2025-11-06		(US20250339810)\|2045-03-27\|(WO2025/230667)\|2027-11-02	(US20250339810)\|Integrated Ocean Alkalinity Enhancement And Seawater Desalination	(US20250339810)\|A desalination unit processes saltwater feedstock (e.g., seawater) to generate freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a high-salt brine stream. An optional pretreatment unit removes contaminants from the saltwater feedstock before desalination. An electrochemical reactor converts the brine stream into a reduced-salt stream having a salt content lower than the saltwater feedstock by converting salt molecules contained in the brine stream into acid molecules contained in an acid product stream and base molecules contained in a base product stream. A mixing device combines the reduced-salt stream with the saltwater feedstock before the resulting mixture solution is delivered to the desalination unit for desalination. The base product stream leaving the electrochemical reactor may be used for ocean alkalinity enhancement (OAE), and the acid product stream may be used to reduce energy costs associated with crushing/grinding alkaline rock in an enhanced ocean weathering (EOW) process.	EBB CARBON	(US20250339810)\|Ebb Carbon, Inc. ([US])\|(WO2025/230667)\|EBB CARBON, INC. ([US])	LORETZ JEREMY\|PELMAN TODD	(US20250339810)\|Loretz Jeremy\|Pelman Todd	(WO2025/230667)\|BEVER, Patrick ([US])	(US20250339810)\|A benefit of this arrangement is that, when ED apparatus 130A is operated such that reduced-salt stream 111A-2 has a salt concentration lower than that of the saltwater feedstock, less saltwater feedstock must be pumped to and processed by the desalination subsystem (not shown in FIG. 2), thereby reducing both operating energy and maintenance costs in at least some cases.\|Moreover, because greenhouse gas concentrations are already at dangerous levels (i.e., the tub is already dangerously full), there is an urgent need for NETs that are capable of significantly reducing atmospheric CO_2 faster than it is being emitted to achieve safe atmospheric concentration levels (i.e., outflow from the tub's drain must be greater than the reduced inflow from the tap to reduce the tub's water to a safe level).\|Therefore, there is a need to supplement emission reductions with the deployment of NETs, which are systems/processes that serve to reduce existing atmospheric greenhouse gas concentrations by, for example, capturing/removing CO_2 from the air and sequestering it for at least 1,000 years.\|A problem with these EOW strategies is that both the crushing/grinding and dispersing processes require a significant amount of energy.\|Accordingly, by utilizing an electrochemical reactor to remove salt from the brine stream generated by the desalination process, and then utilizing the reduced-salt stream generated by the electrochemical reactor to supplement/dilute the saltwater feedstock directed into the desalination unit, the modified desalination system both mitigates the above-mentioned brine disposition problem and addresses other problems associated with conventional desalination systems.\|Note that the pressure required to force freshwater through a membrane is directly proportional to the feedstock solution's salt content (i.e., saltier water having a relatively high salt concentration requires more pressure than less salty water), but this pressure is limited by the strength of the membrane (i.e., the membrane will rupture if the pressure is too high).\|	(US20250339810)\|1. A desalination system for generating a freshwater stream by removing salt from a saltwater feedstock having a first salt concentration level such that the removed salt is concentrated in a brine stream having a second salt concentration level, the second salt concentration level being higher than the first concentration level, the desalination system comprising: an electrochemical reactor configured to generate a reduced-salt stream by electrochemically processing the brine stream such that the salt contained in the brine stream is converted into acid molecules contained in an acid product stream and base molecules contained in a base product stream, and such that the reduced-salt stream exiting the electrochemical reactor has a third salt concentration that is lower than the first salt concentration; a mixing device configured to combine a saltwater feedstock stream including the saltwater feedstock with at least some of the reduced-salt stream to produce a mixture stream having a fourth salt concentration that is between the first and third salt concentrations; and a desalination unit configured to generate the freshwater stream and the brine stream by processing the mixture stream.\|8. A method for generating a freshwater stream by removing salt from a saltwater feedstock having a first salt concentration level such that the removed salt is concentrated in a brine stream having a second salt concentration level, the second salt concentration level being higher than the first concentration level, the method comprising: generating a reduced-salt stream by electrochemically processing the brine stream such that at least some of the salt contained in the brine stream is converted into acid molecules contained in an acid product stream and base molecules contained in a base product stream, and such that the reduced-salt stream has a third salt concentration that is lower than the first salt concentration; generating a mixture stream having a fourth salt concentration that is between the first and third salt concentrations by combining a saltwater feedstock stream including the saltwater feedstock with the reduced-salt stream; and desalinating the mixture stream to generate the freshwater stream and the brine stream.\|16. A hybrid carbon dioxide removal (CDR) system comprising: an ocean alkalinity enhancement (OAE) subsystem including an electrodialysis device configured to electrochemically process salt obtained from an ocean's seawater such that the salt is converted into a base substance and an acid substance, the OAE subsystem further including an alkaline product generator configured to generate an ocean alkalinity product including the base substance fully dissolved in a salt solution; an enhanced ocean weathering (EOW) subsystem configured to generate an alkaline slurry by combining a portion of the acid substance from the electrodialysis device with an alkaline aggregate such that an accelerated ocean weathering reaction between the alkaline aggregate and the acid substance both neutralizes the acid substance and etches/weakens the alkaline aggregate; and a base delivery subsystem configured to supply the ocean alkalinity product and the alkaline slurry to an ocean such that both the fully dissolved base substance and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification.\|	(US20250339810)\|According to another aspect, at least some of the reduced-salt stream generated by the electrochemical process is mixed/combined with the saltwater feedstock (i.e., such that the saltwater feedstock is effectively diluted by the reduced-salt stream before performing the desalination process), thereby reducing freshwater production costs by reducing the amount of salt that must be filtered/removed from the saltwater feedstock during the desalination process (i.e., in comparison to conventional processes in which only saltwater feedstock is desalinated).\|In an embodiment the present invention is directed to a modified desalination process and associated method that utilizes an electrochemical process to both mitigate the above-mentioned brine disposition problem and address other problems associated with conventional desalination systems/methods.\|The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|	(US20250339810)\|OCEAN ALKALINITY(100,4)\|INTEGRATED OCEAN ALKALINITY(100,1)\|ALKALI AGGREGATE(81,27)\|BRINE STREAM(75,40)\|OCEAN ALKALINITY PRODUCT(72,35)\|OCEAN SEAWATER(72,7)\|FRESHWATER STREAM(66,19)\|FEEDSTOCK(61,63)\|ALKALINE SLURRY(61,28)\|ACCELERATED OCEAN(58,9)\|DESALINIZATION(53,24)\|BRINE DISPOSITION(46,7)\|ELECTROCHEMICAL REACTOR(43,68)\|CRUSHING GRIND ALKALINE ROCK(43,1)\|DESALINIZATION SUBSYSTEM(41,21)\|MEMBRANE DESALINIZATION(41,6)\|RAW SEAWATER(39,6)\|ELECTRODIALYSIS(38,61)\|ACIDIC SUBSTANCE(38,21)\|OCEAN ACIDIFICATION(38,14)\|REMOVING SALT(38,5)\|SALT WATER FEEDSTOCK STREAM(38,5)\|BRINE(37,35)\|MIXTURE STREAM(36,19)\|SALT WATER FEEDSTOCK(33,5)\|SEA(31,36)\|SUBSYSTEM(31,30)\|FRESHWATER PRODUCTION(31,1)\|SALT CONCENTRATION(30,47)\|OUTFALL LOCATION(30,8)\|ACIDIC BUFFER TANK(29,20)\|OCEAN SEAWATER PH LEVEL(29,3)\|TUB DRAIN(29,2)\|ION EXCHANGE MEMBRANE(27,16)\|SEAWATER DESALINIZATION SUBSYSTEM(27,6)\|ETCHED WEAKENED ALKALINE AGGREGATE(27,3)\|ACIDIC PRODUCT STREAM(26,14)\|SALT CONCENTRATION LEVEL(26,4)\|CONCENTRATION LEVEL(26,2)\|GENERATED FRESHWATER(26,2)\|SALT INFLOW RATE(26,2)\|SLURRY GENERATOR(25,8)\|SALTY WATER(25,2)\|FEEDSTOCK SOLUTION SALT CONTENT(25,1)\|MODIFIED DESALINIZATION(23,8)\|ALKALINE PRODUCT GENERATOR(23,2)\|TUB WATER(23,1)\|BASE SUBSTANCE(22,26)\|CONSTANT OUTFLOW(22,3)\|GREENHOUSE GAS ATMOSPHERE(21,2)\|ALKALINE AGGREGATE CAPTURE REDUCE(20,3)\|BASE PRODUCT STREAM(19,18)\|DEPLOYMENT(19,2)\|AQUEOUS ACID SOLUTION(18,13)\|FLUID BUFFERING(18,12)\|BASE DELIVERY SUBSYSTEM(18,7)\|HYBRID CARBON DIOXIDE(18,3)\|SALT CONVERSION(18,2)\|REDUCING AGENT INFLOW(18,1)\|SAFE ATMOSPHERIC CONCENTRATION LEVEL(18,1)\|REDUCED SALT STREAM(17,56)\|FRESHWATER(17,22)\|CHLORIDE ION(17,11)\|DESALINIZATION(17,11)\|SOLUTION SALT CONTENT(17,1)\|URGENT NEED(17,1)\|GREENHOUSE GAS(16,6)\|ATMOSPHERIC CARBON DIOXIDE(16,5)\|BRINY GROUNDWATER(16,5)\|STRATEGY(16,2)\|OCEAN ALKALINITY ENHANCEMENT(15,58)\|BASE BUFFER TANK(15,23)\|ION EXCHANGE STACK(15,19)\|CRUSHING GRINDING(15,4)\|OPPOSING ELECTRODE(15,4)\|INTEGRATING SEAWATER DESALINIZATION(15,2)\|OCEAN SEAWATER ALKALINITY(15,2)\|SALT BRINE STREAM(15,2)\|TUB(15,2)\|DESALINIZATION UNIT(14,42)\|ENHANCED OCEAN WEATHERING(14,38)\|ELECTROCHEMICAL(14,14)\|DANGEROUS LEVEL(14,2)\|DISPERSING(14,1)\|CARBON DIOXIDE(13,12)\|PARTY BUYER(13,6)\|IRRIGATION(13,4)\|OUTFLOW(13,4)\|REACTION TANK(12,7)\|BYPRODUCT BRINE STREAM(12,3)\|EMISSION REDUCTION(12,1)\|BIPOLAR ELECTRODIALYSIS(11,31)\|AQUEOUS BASE SOLUTION(11,13)\|MODIFIED DESALINIZATION(11,3)\|SAFE LEVEL(11,2)\|CATASTROPHIC OCEAN ACIDIFICATION(11,1)\|INTEGRATED DESALINIZATION OCEAN ALKALINITY ENHANCEMENT(10,8)\|COASTAL COMMUNITY(10,2)\|UNPROCESSED BRINE BUILDUP(10,1)\|MIXING TANK(9,10)\|SALT SOLUTION(9,8)\|SUPPLYING ELECTRICITY(9,6)\|OCEAN CAPTURE(9,4)\|ECOLOGICAL HAZARD(9,2)\|SEAWATER DESALINIZATION PLANT(9,2)\|STAND ALONE SEAWATER DESALINIZATION(9,2)\|NEGATIVE EMISSIONS TECHNOLOGIE(8,14)\|HUMAN CONSUMPTION(8,8)\|SALT FEEDSTOCK SOLUTION(8,5)\|MIXTURE SOLUTION(8,4)\|OUTFLOW PORT(8,4)\|ACCELERATED WEATHERING(8,3)\|REVERSE OSMOSIS SEAWATER DESALINIZATION(8,1)\|SHELLFISH DECREASED SURVIVAL(8,1)\|REDUCE SALT STREAM(7,18)\|SODIUM ION(7,10)\|ACIDIC BYPRODUCT(7,4)\|PROCESS FLUID(7,4)\|FILTERED SEAWATER BRINE(7,2)\|LCOC RATING(7,2)\|MINIMIZING LCOC(7,2)\|SALT DISSOCIATION(7,2)\|ALKALINE ROCK CRUSHING GRINDING(7,1)\|BRACKISH GROUNDWATER(7,1)\|DIRECTLY PROPORTIONAL(7,1)\|FEEDSTOCK PRETREATMENT(7,1)\|FRESHWATER AQUIFER(7,1)\|OCEAN DEACIDIFICATION(7,1)\|CARBON DIOXIDE REMOVAL(6,14)\|INPUT MANIFOLD(6,6)\|ELECTROLYTE SOLUTION(6,5)\|CONTAINING PLASTIC(6,3)\|DIVALENT ION(6,3)\|FRESHWATER OUTPUT STREAM(6,3)\|INFLOW PORT(6,3)\|SEMIPERMEABLE MEMBRANE(6,3)\|FEEDSTOCK INFLOW RATE(6,2)\|FILTERING CONTAMINANT(6,2)\|SPOT PRICING(6,2)\|BATHTUB ANALOGY(6,1)\|COORDINATE DESALINIZATION(6,1)\|CRUSHING GRINDING ALKALINE AGGREGATE(6,1)\|ECOLOGICAL CONCERN(6,1)\|GOVERNMENT AUTHORIZATION(6,1)\|OCEAN DISPERSION(6,1)\|OUTFALL BRINE INCREASED SALINITY(6,1)\|PHYSIOLOGICAL CHALLENGE(6,1)\|PROTON DISSOCIATION(6,1)\|SEAWATER FEEDSTOCK SALT CONTENT(6,1)\|SEAWATER HARDNESS(6,1)\|SHARED PLANT FACILITY(6,1)\|WATERTIGHT CONTAINMENT HOUSING(6,1)\|WEAKENED ETCHED ALKALINE AGGREGATE(6,1)\|WIDESPREAD ACCEPTANCE(6,1)\|POST PRODUCTION(5,12)\|MAINTENANCE COST(5,11)\|NAOH(5,10)\|ACIDIC SOLUTION(5,9)\|WEAK ACID STREAM(5,8)\|AQUEOUS SOLUTION(5,7)\|ACIDIC STREAM(5,4)\|CELL ACID CHAMBER(5,4)\|CELL SALT CHAMBER(5,4)\|DESALINIZATION SYSTEM METHOD(5,2)\|FINAL ALKALINE SLURRY(5,2)\|LEAVING REACTOR(5,2)\|MOTIVE(5,2)\|SALT AQUEOUS FEEDSTOCK SOLUTION(5,2)\|DECREASED SEAWATER PH(5,1)\|DISSOCIATED HYDROXIDE ION(5,1)\|DISSOLUTION KINETICS(5,1)\|ETCHED WEAKENED AGGREGATE(5,1)\|MANKIND EFFORT(5,1)\|NEARBY OCEAN(5,1)\|OCEAN ALKALINITY PRODUCT GENERATION(5,1)\|PRECRUSHED GROUND ALKALINE AGGREGATE(5,1)\|PREINDUSTRIAL ERA TEMPERATURE(5,1)\|RAW FEEDSTOCK(5,1)\|REDUCING ECOSAFETY RISK(5,1)\|SEAWATER FEEDSTOCK INPUT(5,1)\|TARGETED CONTAMINANT(5,1)\|UNTREATED FEEDSTOCK(5,1)\|SYSTEM CONTROLLER(4,20)\|ANODE(4,5)\|ENERGY COST(4,3)\|OUTPUT MANIFOLD(4,3)\|SALT BUFFER TANK(4,3)\|TREATED UNTREATED SALT(4,3)\|NANOFILTRATION(4,2)\|ALKALINE AGGREGATE DELIVERY INJECTION(4,1)\|ALKALINE AGGREGATE ROCK(4,1)\|ALKALINE ROCK AGGREGATE(4,1)\|AMBIENT SEA(4,1)\|BIPOLAR MEMBRANE(4,1)\|BRINE CONVERSION(4,1)\|BYPRODUCT STREAM(4,1)\|COARSELY GROUND ALKALINE AGGREGATE(4,1)\|DESALINIZED FLUID(4,1)\|EARTH OCEAN(4,1)\|ELECTROCHEMICAL CONVERSION(4,1)\|HARDNESS RELATED MINERAL HRM(4,1)\|INFLOW SUM(4,1)\|INSTALLATION EXPENSE(4,1)\|PERIODIC MAINTENANCE(4,1)\|PIPE INTERCONNECTION(4,1)\|RECLAIMED METAL SALE(4,1)\|SALT BRINE DISPOSITION(4,1)\|SALT HARDNESS(4,1)\|SILICATE ROCK(4,1)\|SPLIT BRINE(4,1)\|TOTE TANK(4,1)\|TUB FILL(4,1)\|WATER STRESSED COMMUNITY RESILIENCE(4,1)\|HCL(3,13)\|WEAK BASE STREAM(3,7)\|ACID BUFFER TANK(3,6)\|ELECTROCHEMICAL OCEAN ALKALINITY ENHANCEMENT(3,6)\|AQUEOUS SALT SOLUTION(3,5)\|ACID PRODUCTION TANK(3,4)\|BASE PRODUCT TANK(3,3)\|CATHODE(3,3)\|FOSSIL FUEL(3,3)\|ION EXCHANGE FILTER(3,3)\|RESERVOIR(3,3)\|ACIDIC PRODUCT NEUTRALIZATION(3,2)\|BRINE SOLUTION(3,2)\|EMISSION RATE(3,2)\|ION CURRENT(3,2)\|MARINE ORGANISM(3,2)\|OUTFLOW RATE(3,2)\|POSITIVE ELECTRODE(3,2)\|SODIUM TRANSFER(3,2)\|SUPPLYING ENERGY(3,2)\|ULTRAFILTRATION(3,2)\|ACID DISPOSAL(3,1)\|ALKALI PARTICLE(3,1)\|ALKALINE OCEAN PRODUCT(3,1)\|ALKALINE PRODUCTION GENERATOR(3,1)\|ALKALINE SUBSTANCE(3,1)\|BIOPHYSICAL LIMIT(3,1)\|BUFFER RESOURCE(3,1)\|CALCIUM CARBONATE SHELL(3,1)\|CELL SALT INLET(3,1)\|CELL SALT OUTLET(3,1)\|CHLORINE ION(3,1)\|CIRCLED ARROW(3,1)\|CONTINUING DEVELOPMENT(3,1)\|DIRECTLY REVERSE OCEAN ACIDIFICATION(3,1)\|DRASTIC REDUCTION(3,1)\|EARTH ATMOSPHERE(3,1)\|ECONOMIC REASON(3,1)\|ELECTROCHEMICAL PROCESSING(3,1)\|FINAL SALINITY(3,1)\|FRESHWATER NATURAL MOVEMENT(3,1)\|ION PERMEABLE MEMBRANE(3,1)\|LCOCS(3,1)\|LEAVING ELECTROCHEMICAL REACTOR(3,1)\|LIQUID FRESHWATER(3,1)\|MAFICS ULTRAMAFICS(3,1)\|MAINTAINING PRETREATMENT COST(3,1)\|MAJOR CHALLENGE(3,1)\|MEMBRANE B1(3,1)\|MINIMIZING SALT CONTENT(3,1)\|MIXING OUTLET(3,1)\|NET BENEFIT(3,1)\|OCEAN ABILITY(3,1)\|ONLY SALT(3,1)\|OUTLET MANIFOLD(3,1)\|PRECRUSHER GRINDER(3,1)\|PREGRINDING CRUSHING(3,1)\|PRODUCTION EFFICIENCY OPTIMIZATION(3,1)\|PROJECT WIDE OPTIMIZATION(3,1)\|REDUCING LCOC(3,1)\|SEAWATER DESALINIZATION(3,1)\|SEAWATER TREATMENT(3,1)\|SHARED SALT(3,1)\|SLOW INFLOW RATE(3,1)\|WATER INFLOW(3,1)\|112E 31 ROCK AGGREGATE(2,1)\|ACID DOSING PUMP(2,1)\|ADDRESSING(2,1)\|ADVANCED WEATHERING OPERATION VALUABLE(2,1)\|AQUEOUS ACID(2,1)\|AQUEOUS ALKALINE SOLUTION(2,1)\|ARTIFICIAL INTELLIGENCE(2,1)\|BICARBONATE(2,1)\|BUFFERING(2,1)\|CAPITAL EXPENSE REDUCTION(2,1)\|CARBON DIOXIDE TON(2,1)\|CELL ACID INLET(2,1)\|CELL ACID OUTLET(2,1)\|\|(WO2025/230667)\|ALKALI AGGREGATE(100,25)\|SEAWATER DESALINIZATION(100,13)\|OCEAN ALKALINITY(100,7)\|INTEGRATED OCEAN ALKALINITY(100,3)\|BRINE STREAM(91,40)\|OCEAN ALKALINITY PRODUCT(87,35)\|NEUTRALI ZES(81,1)\|FRESHWATER STREAM(80,19)\|OCEAN ACIDI FICATION(80,4)\|ALKALINE SLURRY(74,27)\|ACCELERATED OCEAN(71,9)\|FEEDSTOCK(68,63)\|DESALINIZATION(64,24)\|UTILI ZING(62,5)\|WIDESPREAD ACCEPTANCE(57,1)\|BRINE DISPOSITION(56,7)\|CRUSHING GRIND ALKALINE ROCK(53,1)\|ELECTROCHEMICAL REACTOR(52,70)\|MANKIND EFFORT(51,1)\|MEMBRANE DESALINIZATION(49,6)\|ACIDIC SUBSTANCE(48,17)\|RAW SEAWATER(47,6)\|ELECTRODIALYSIS(45,62)\|REMOVING SALT(45,5)\|SALT WATER FEEDSTOCK STREAM(45,5)\|SEA(44,38)\|BRINE(44,35)\|MIXTURE STREAM(44,19)\|OCEAN ACIDIFICATION(41,10)\|SALT WATER FEEDSTOCK(40,5)\|FRESHWATER PRODUCTION(38,1)\|SUBSYSTEM(37,31)\|OUTFALL LOCATION(36,8)\|SALT CONCENTRATION(35,48)\|TUB DRAIN(35,2)\|SEAWATER(34,32)\|ION EXCHANGE MEMBRANE(33,16)\|SEAWATER DESALINIZATION SUBSYSTEM(33,6)\|ETCHED WEAKENED ALKALINE 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TECHNOLOGIE(12,14)\|ATMOSPHERIC CO2(12,9)\|ACID BUFFER TANK(12,8)\|COASTAL COMMUNITY(12,2)\|GOVERNMENT AUTHORI ZATION(12,1)\|UNPROCESSED BRINE BUILDUP(12,1)\|CARBON DIOXIDE REMOVAL(11,15)\|MIXING TANK(11,10)\|SALT SOLUTION(11,8)\|SUPPLYING ELECTRICITY(11,6)\|OCEAN CAPTURE(11,4)\|ECOLOGICAL HAZARD(11,2)\|SEAWATER DESALINIZATION PLANT(11,2)\|STAND ALONE SEAWATER DESALINIZATION(11,2)\|SUF FICIENT(11,2)\|UTILI ZED(11,2)\|UTILI ZES(11,2)\|ELECTROCHEMICAL ASSISTED OCEAN(11,1)\|SPECI FIC MODIFIED DESALINIZATION(11,1)\|HUMAN CONSUMPTION(10,8)\|SALT FEEDSTOCK SOLUTION(10,5)\|MIXTURE SOLUTION(10,4)\|OUTFLOW PORT(10,4)\|ACCELERATED WEATHERING(10,3)\|ALKALINE AGGREGATE NEUTRALI(10,1)\|MODI FICATION(10,1)\|REVERSE OSMOSIS SEAWATER DESALINIZATION(10,1)\|SHELLFISH DECREASED SURVIVAL(10,1)\|PROCESS FLUID(9,4)\|ETCHED WEAKENED AGGREGATE(9,2)\|SALT DISSOCIATION(9,2)\|ALKALINE ROCK CRUSHING GRINDING(9,1)\|BRACKISH GROUNDWATER(9,1)\|CONFIGURING POSTPRODUCTION(9,1)\|DIRECTLY PROPORTIONAL(9,1)\|EF FECTIVENESS(9,1)\|FEEDSTOCK PRETREATMENT(9,1)\|FRESHWATER AQUIFER(9,1)\|NEUTRALI ZED(9,1)\|OCEAN DEACIDIFICATION(9,1)\|SYSTEM FEATURE(9,1)\|SODIUM ION(8,10)\|ELECTROLYTE SOLUTION(8,5)\|FILTERED SEAWATER BRINE(8,2)\|NAOH(7,10)\|CONTAINING PLASTIC(7,3)\|DIVALENT ION(7,3)\|FRESHWATER OUTPUT STREAM(7,3)\|INFLOW PORT(7,3)\|DESALINIZATION SYSTEM METHOD(7,2)\|FEEDSTOCK INFLOW RATE(7,2)\|FILTERING CONTAMINANT(7,2)\|SPOT PRICING(7,2)\|BATHTUB ANALOGY(7,1)\|COORDINATE DESALINIZATION(7,1)\|CRUSHING GRINDING ALKALINE AGGREGATE(7,1)\|ECOLOGICAL CONCERN(7,1)\|MINIMI ZES(7,1)\|MINIMI ZING SALT CONTENT(7,1)\|OCEAN DISPERSION(7,1)\|OUTFALL BRINE INCREASED SALINITY(7,1)\|PHYSIOLOGICAL CHALLENGE(7,1)\|PROTON DISSOCIATION(7,1)\|SEAWATER FEEDSTOCK SALT CONTENT(7,1)\|SEAWATER HARDNESS(7,1)\|SHARED PLANT FACILITY(7,1)\|WATERTIGHT CONTAINMENT HOUSING(7,1)\|WEAKENED ETCHED ALKALINE AGGREGATE(7,1)\|ACIDIC SOLUTION(6,9)\|WEAK ACID STREAM(6,8)\|AQUEOUS SOLUTION(6,7)\|ACIDIC STREAM(6,4)\|CELL ACID CHAMBER(6,4)\|CELL SALT CHAMBER(6,4)\|INPUT MANIFOLD(6,4)\|ACIDIC BYPRODUCT(6,2)\|ECO SAFETY RISK(6,2)\|INPUT MANI FOLD(6,2)\|LEAVING REACTOR(6,2)\|MOTIVE(6,2)\|SALT AQUEOUS FEEDSTOCK SOLUTION(6,2)\|SEMIPERMEABLE MEMBRANE(6,2)\|ADJ USTS(6,1)\|ALKALINE AGGREGATE INJECTION(6,1)\|CUTTING CO2 EMISSION(6,1)\|DECREASED SEAWATER PH(6,1)\|DISSOCIATED HYDROXIDE ION(6,1)\|DISSOLUTION KINETICS(6,1)\|ECOSAFETY RISK(6,1)\|ELECTROCHEMICAL REACTOR HOD(6,1)\|LCOC RATING(6,1)\|MINIMIZING LCOC(6,1)\|NEARBY OCEAN(6,1)\|OCEAN ALKALINITY PRODUCT GENERATION(6,1)\|OPTIMI ZE(6,1)\|PRECRUSHED GROUND ALKALINE AGGREGATE(6,1)\|PREINDUSTRIAL ERA TEMPERATURE(6,1)\|RAW FEEDSTOCK(6,1)\|SEAWATER FEEDSTOCK INPUT(6,1)\|SETTING ENERGY OCEAN DISPERSAL(6,1)\|TARGETED CONTAMINANT(6,1)\|UNTREATED FEEDSTOCK(6,1)\|POST PRODUCTION(5,8)\|ENERGY COST(5,3)\|SALT BUFFER TANK(5,3)\|TREATED UNTREATED SALT(5,3)\|NANOFILTRATION(5,2)\|ABSORBED CO2(5,1)\|ALKALINE AGGREGATE ROCK(5,1)\|BIPOLAR MEMBRANE(5,1)\|BRINE CONVERSION(5,1)\|BYPRODUCT STREAM(5,1)\|CAPTURED CO2(5,1)\|CO2 DISSOLUTION(5,1)\|COARSELY GROUND ALKALINE AGGREGATE(5,1)\|DESALINIZED FLUID(5,1)\|EARTH OCEAN(5,1)\|HARDNESS RELATED MINERAL HRM(5,1)\|INFLOW SUM(5,1)\|INSTALLATION EXPENSE(5,1)\|MEMBRANE FL(5,1)\|NEGATIVE CO2 EMISSION(5,1)\|OCEAN SEAWATER PH LEVEL(5,1)\|PERIODIC MAINTENANCE(5,1)\|PIPE INTERCONNECTION(5,1)\|RECLAIMED METAL SALE(5,1)\|SALT BRINE DISPOSITION(5,1)\|SALT HARDNESS(5,1)\|SILICATE ROCK(5,1)\|SPLIT BRINE(5,1)\|TOTE TANK(5,1)\|TUB FILL(5,1)\|WATER STRESSED COMMUNITY RESILIENCE(5,1)\|WEAK BASE STREAM(4,7)\|AQUEOUS SALT SOLUTION(4,5)\|ACID PRODUCTION TANK(4,4)\|ANODE(4,4)\|ACIDIC PRODUCT NEUTRALIZATION(4,2)\|BRINE SOLUTION(4,2)\|HYBRID CARBON DIOXIDE(4,2)\|ION CURRENT(4,2)\|MARINE ORGANISM(4,2)\|OUTFLOW RATE(4,2)\|OUTPUT MANIFOLD(4,2)\|POSITIVE ELECTRODE(4,2)\|SIGNI(4,2)\|SODIUM TRANSFER(4,2)\|ULTRAFILTRATION(4,2)\|ALKALI PARTICLE(4,1)\|ALKALINE OCEAN PRODUCT(4,1)\|ALKALINE PRODUCTION GENERATOR(4,1)\|BIOPHYSICAL LIMIT(4,1)\|BUFFER RESOURCE(4,1)\|CALCIUM CARBONATE SHELL(4,1)\|CELL SALT INLET(4,1)\|CELL SALT OUTLET(4,1)\|CHLORINE ION(4,1)\|CIRCLED ARROW(4,1)\|DIRECTLY REVERSE OCEAN ACIDIFICATION(4,1)\|DRASTIC REDUCTION(4,1)\|EARTH ATMOSPHERE(4,1)\|ECONOMIC REASON(4,1)\|ELECTROCHEMICAL PROCESSING(4,1)\|F EEDSTOCK STREAM(4,1)\|FINAL SALINITY(4,1)\|FRESHWATER NATURAL MOVEMENT(4,1)\|ION PERMEABLE MEMBRANE(4,1)\|LCOCS(4,1)\|LEAVING ELECTROCHEMICAL REACTOR(4,1)\|LIQUID FRESHWATER(4,1)\|MAINTAINING PRETREATMENT COST(4,1)\|MAJOR CHALLENGE(4,1)\|MIXING OUTLET(4,1)\|NET BENEFIT(4,1)\|OCEAN ABILITY(4,1)\|ONLY SALT(4,1)\|OUTLET MANIFOLD(4,1)\|OUTPUT MANI FOLD(4,1)\|PRECRUSHER GRINDER(4,1)\|PRODUCTION EFFICIENCY OPTIMIZATION(4,1)\|PROJECT WIDE OPTIMIZATION(4,1)\|REDUCING CO2 EMISSION(4,1)\|REDUCING LCOC(4,1)\|SEAWATER DESALINIZATION(4,1)\|SEAWATER TREATMENT(4,1)\|SENSOR SI(4,1)\|SHARED SALT(4,1)\|SLOW INFLOW RATE(4,1)\|THREAT(4,1)\|WATER INFLOW(4,1)\|ZE SENSOR(4,1)\|MAINTENANCE COST(3,11)\|ELECTROCHEMICAL OCEAN ALKALINITY ENHANCEMENT(3,6)\|BASE PRODUCT TANK(3,3)\|CATHODE(3,3)\|FOSSIL FUEL(3,3)\|ION EXCHANGE FILTER(3,3)\|RESERVOIR(3,3)\|ACID DOSING PUMP(3,1)\|ADDRESSING(3,1)\|AQUEOUS ALKALINE SOLUTION(3,1)\|	(US20250339810)\|1. A desalination system for generating a freshwater stream by removing salt from a saltwater feedstock having a first salt concentration level such that the removed salt is concentrated in a brine stream having a second salt concentration level, the second salt concentration level being higher than the first concentration level, the desalination system comprising:\| an electrochemical reactor configured to generate a reduced-salt stream by electrochemically processing the brine stream such that the salt contained in the brine stream is converted into acid molecules contained in an acid product stream and base molecules contained in a base product stream, and such that the reduced-salt stream exiting the electrochemical reactor has a third salt concentration that is lower than the first salt concentration;\| a mixing device configured to combine a saltwater feedstock stream including the saltwater feedstock with at least some of the reduced-salt stream to produce a mixture stream having a fourth salt concentration that is between the first and third salt concentrations; and\| a desalination unit configured to generate the freshwater stream and the brine stream by processing the mixture stream.\|2. The system of claim 1, further comprising a pretreatment unit configured to generate the saltwater feedstock stream by removing contaminants from a portion of the saltwater feedstock received from an external source.\|3. The system of claim 2, wherein the mixing device is configured such that the mixture stream includes all of the reduced-salt stream received from the electrochemical reactor and such that the mixture stream exiting the mixing device is maintained at a constant outflow rate by adjusting an inflow rate of the saltwater feedstock stream entering the mixing device.\|4. The system of claim 1, wherein the desalination unit comprises one of a thermal desalination system and a membrane-based desalination system.\|5. The system of claim 1, wherein the electrochemical reactor comprises:\| an electrodialysis (ED) apparatus including an ion exchange stack comprising a plurality of chambers arranged in series between opposing electrodes and respectively separated by intervening ion exchange membranes; and\| a flow control system configured to direct the brine stream to a first chamber of the plurality of chambers and to direct the reduced-salt stream from said first chamber, to direct an aqueous acid solution to a second chamber of the plurality of chambers and to direct said acid product stream away from said second chamber, and to direct an aqueous base solution to a third chamber of the plurality of chambers and to direct said base product stream away from said third chamber,\| wherein the ED apparatus is configured such that chloride ions disposed in the brine stream pass from the first chamber through a first ion exchange membrane into the second chamber, and such that sodium ions disposed in the brine stream pass from the first chamber through a second ion exchange membrane into the third chamber.\|6. The system of claim 5, wherein the electrochemical reactor further comprises a fluid buffering system including:\| an acid buffer tank configured to contain the aqueous acid solution directed into said second chamber of the ED apparatus and to receive a first portion of the acid product stream directed away from said second chamber of the ED apparatus; and\| a base buffer tank configured to contain the aqueous base solution directed into said third chamber of the ED apparatus and to receive a first portion of the base product stream directed away from said third chamber of the ED apparatus,\| wherein the flow control system is further configured to direct a portion of the generated freshwater into one or more of said acid buffer tank and said base buffer tank.\|7. The system of claim 1,\| wherein the saltwater feedstock comprises raw seawater obtained from an ocean,\| wherein the system further comprises a post-production unit including at least one of:\| an alkalinity product generation unit configured to generate an ocean alkalinity product using at least a portion of the base product stream such that the ocean alkalinity product includes said base molecules fully dissolved in a salt solution and has a pH level that is a predetermined amount higher than a pH level of the ocean's seawater;\| an enhanced ocean weathering subsystem configured to generate an alkaline slurry using at least a portion of the acid product stream by combining the acid product stream portion with an alkaline aggregate such that a reaction between the alkaline aggregate and the acid molecules both neutralizes the acid molecules and etches the alkaline aggregate; and\| a base delivery system configured to supply at least one of the ocean alkalinity product and the alkaline slurry to the ocean at a designated outfall location.\|8. A method for generating a freshwater stream by removing salt from a saltwater feedstock having a first salt concentration level such that the removed salt is concentrated in a brine stream having a second salt concentration level, the second salt concentration level being higher than the first concentration level, the method comprising:\| generating a reduced-salt stream by electrochemically processing the brine stream such that at least some of the salt contained in the brine stream is converted into acid molecules contained in an acid product stream and base molecules contained in a base product stream, and such that the reduced-salt stream has a third salt concentration that is lower than the first salt concentration;\| generating a mixture stream having a fourth salt concentration that is between the first and third salt concentrations by combining a saltwater feedstock stream including the saltwater feedstock with the reduced-salt stream; and\| desalinating the mixture stream to generate the freshwater stream and the brine stream.\|9. The method of claim 8, further comprising generating the saltwater feedstock stream by removing contaminants from a portion of the saltwater feedstock received from an external source.\|10. The method of claim 9, wherein generating the mixture stream comprises utilizing all of the reduced-salt stream received from the electrochemical reactor and maintaining the mixture stream at a constant outflow rate by adjusting an inflow rate of the saltwater feedstock stream.\|11. The method of claim 8, wherein desalinating the mixture stream comprises utilizing one of a thermal desalination system and a membrane-based desalination system.\|12. The method of claim 8, wherein generating a reduced-salt stream comprises:\| directing the brine stream through a first chamber while directing an aqueous acid solution to a second chamber and directing an aqueous base solution to a third chamber, the first chamber being disposed between the second chamber and the third chamber;\| applying an electric field across the first, second and third chambers such that chloride ions disposed in the brine stream pass from the first chamber through a first ion exchange membrane into the second chamber, and such that sodium ions disposed in the brine stream pass from the first chamber through a second ion exchange membrane into the third chamber.\|13. The method of claim 12, further comprising:\| directing the aqueous acid solution from an acid buffer tank into said second chamber and directing a first portion of the acid product stream exiting the second chamber to the acid buffer tank;\| directing the aqueous base solution from a base buffer tank into said third chamber and directing a first portion of the base product stream exiting the third chamber to the base buffer tank; and\| directing a portion of the generated freshwater into one or more of said acid buffer tank and said base buffer tank.\|14. The method of claim 8,\| wherein the saltwater feedstock comprises raw seawater obtained from an ocean, and\| wherein the method further comprises:\| generating an ocean alkalinity product using at least a portion of the base product stream such that the ocean alkalinity product includes said base molecules fully dissolved in a salt solution and has a pH level that is a predetermined amount higher than a pH level of the ocean's seawater; and\| supplying the ocean alkalinity product to the ocean at a designated outfall location.\|15. The method of claim 8,\| wherein the saltwater feedstock comprises raw seawater obtained from an ocean, and\| wherein the method further comprises:\| generating an alkaline slurry by combining at least a portion of the base product stream with analkaline aggregate such that a reaction between the alkaline aggregate and the acid molecules both neutralizes the acid molecules and etches the alkaline aggregate; and\| supplying the alkaline slurry to the ocean at a designated outfall location.\|16. A hybrid carbon dioxide removal (CDR) system comprising:\| an ocean alkalinity enhancement (OAE) subsystem including an electrodialysis device configured to electrochemically process salt obtained from an ocean's seawater such that the salt is converted into a base substance and an acid substance, the OAE subsystem further including an alkaline product generator configured to generate an ocean alkalinity product including the base substance fully dissolved in a salt solution;\| an enhanced ocean weathering (EOW) subsystem configured to generate an alkaline slurry by combining a portion of the acid substance from the electrodialysis device with an alkaline aggregate such that an accelerated ocean weathering reaction between the alkaline aggregate and the acid substance both neutralizes the acid substance and etches/weakens the alkaline aggregate; and\| a base delivery subsystem configured to supply the ocean alkalinity product and the alkaline slurry to an ocean such that both the fully dissolved base substance and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification.\|17. The hybrid CDR system of claim 16, wherein the EOW subsystem comprises:\| an accelerated ocean weathering reaction apparatus includes a reaction tank configured to contain a process fluid including a mixture of the alkaline aggregate and acid substance portion until the accelerated ocean weathering reaction is completed; and\| a slurry generator configured to generate the alkaline slurry by processing the etched/weakened alkaline aggregate contained in the process fluid received from the accelerated ocean weathering reaction apparatus.\|18. The hybrid CDR system of claim 17, wherein the slurry generator further is further configured to separate (reclaim) one or more metal elements from the alkaline slurry.\|19. The hybrid CDR system of claim 16, further comprising:\| a mixing device configured to combine a saltwater feedstock stream including the ocean's seawater with the base substance exiting the electrodialysis device to produce a mixture stream; and\| a desalination unit configured to generate a freshwater stream and a brine stream by processing the mixture stream.\|20. The hybrid CDR system of claim 19, wherein electrodialysis device is configured to receive and electrochemically process salt contained in the brine stream.	(US20250339810)\|RELATED APPLICATIONS/PATENTS\|[0001] This application claims priority from U.S. Provisional Patent Application No. 63/716,029, entitled “Integrated Ocean Alkalinity Enhancement And Seawater Desalination”, filed on Nov. 4, 2024, which is entirely incorporated herein by reference.\|[0002] This application also claims priority from U.S. Provisional Patent Application No. 63/641,910, entitled “Electrochemical Assisted Ocean Weathering”, filed on May 2, 2024, which is entirely incorporated herein by reference.\|(US20250339810)\|FIELD OF THE INVENTION\|[0003] The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|BACKGROUND\|[0004] As humans burn more and more fossil fuels, the resulting increased carbon dioxide (CO2) concentration in Earth's atmosphere causes both climate change and ocean acidification. The increased atmospheric concentrations of CO2 and other greenhouse gases (e.g., methane) produces climate change by trapping heat close to earth's surface, thereby increasing both air and sea temperatures. Because earth's oceans absorb about 25% of atmospheric CO2, and because the absorbed CO2 dissolves to form carbonic acid that remains trapped in the seawater, the increased atmospheric CO2 concentration caused by burning fossil fuels also produces ocean acidification by way of increasing the amount of CO2 gas dissolved in the ocean.\|[0005] Both climate change and ocean acidification pose Climate change in the form significant threats to humans. of increased global average temperatures can produce several dangerous effects such as the loss of polar ice and corresponding increased sea levels, disease, wildfires and stronger storms and hurricanes. Ocean acidification changes the ocean chemistry that most marine organisms rely on. One concern with ocean acidification is that the decreased seawater pH can lead to the decreased survival of shellfish and other aquatic life having calcium carbonate shells, as well as some other physiological challenges for marine organisms.\|[0006] To avoid dangerous climate change, the international Paris Agreement aims to limit the increase in global average temperature to no more than 1.5° C. to 2° C. above the temperatures of the pre-industrial era. Global average temperatures have already increased by between 0.8° C. and 1.2° C. The Intergovernmental Panel on Climate Change (IPCC) estimates that a ‘carbon budget’ of about 500 GtCO2 (billion tons of carbon dioxide), which corresponds to about ten years at current emission rates, provides a 66% chance of limiting climate change to 1.5° C.\|[0007] In addition to cutting CO2 emissions by curtailing the use of fossil fuels, climate models predict that a significant deployment of Negative Emissions Technologies (NETs) will be needed to avoid catastrophic ocean acidification and global warming beyond 1.5° C. (see “Biophysical and economic limits to negative CO2 emissions”, Smith P. et al., Nat. Clim. Chang. 2016; 6:42-50). Current atmospheric CO2 and other greenhouse gas concentrations are already at dangerous levels, so even a drastic reduction in greenhouse gas emissions would merely curtail further increases, not reduce atmospheric greenhouse gas concentrations to safe levels. Moreover, the reduction or elimination of certain greenhouse gas sources (e.g., emissions from long-distance airliners) would be extremely disruptive and/or expensive and are therefore unlikely to occur soon.\|[0008] Therefore, there is a need to supplement emission reductions with the deployment of NETs, which are systems/processes that serve to reduce existing atmospheric greenhouse gas concentrations by, for example, capturing/removing CO2 from the air and sequestering it for at least 1,000 years. The need for NETs may be explained using a bathtub analogy in which atmospheric CO2 is represented by water contained in a bathtub, ongoing CO2 emissions are represented by water flowing into the tub, and NETs are represented by processes that control water outflow through the tub's drain. In this analogy, reduced CO2 emission rates are represented by partially turning off the water inflow tap—the slower inflow rate provides more time before the tub fills, but the tub's water level will continue to rise and eventually overflow. Using this analogy, although reducing CO2 emissions may slow the increase of greenhouse gas in the atmosphere, critical concentration levels will eventually be reached unless NETs are implemented that can offset the reduced CO2 emission level (i.e., remove atmospheric CO2 at the same rate it is being emitted). Moreover, because greenhouse gas concentrations are already at dangerous levels (i.e., the tub is already dangerously full), there is an urgent need for NETs that are capable of significantly reducing atmospheric CO2 faster than it is being emitted to achieve safe atmospheric concentration levels (i.e., outflow from the tub's drain must be greater than the reduced inflow from the tap to reduce the tub's water to a safe level).\|[0009] NETs can be broadly characterized as Direct Air Capture (DAC) approaches and Ocean Capture approaches. DAC approaches utilize natural (e.g., reforestation) and technology-based methods to extract CO2 directly from the atmosphere. Ocean capture approaches utilize various natural and/or technological processes to remove CO2 from the atmosphere and store it in the ocean as bicarbonate, a form of carbon storage that is stable for over 10,000 years.\|[0010] Electrochemical ocean alkalinity enhancement (electrochemical OAE or EOAE) represents an especially promising ocean capture approach that both reduces atmospheric CO2 and mitigates ocean acidification by generating an ocean alkalinity product (i.e., an aqueous alkaline solution containing a fully dissolved base substance) and supplying the ocean alkalinity product to ocean seawater at a designated outfall location. Electrochemical OAE systems typically generate the required base substance using an electrochemical reactor referred to as a bipolar electrodialysis device (BPED), which generally includes an electrodialysis (ED) apparatus and associated flow control devices configured to perform an electrochemical salt-conversion process that converts salt supplied in an aqueous salt feedstock solution (e.g., seawater) into the base substance and an acid substance. The base substance produced by the BPED is then incorporated into the ocean alkalinity (base) product that is then supplied to the ocean. As the base substance diffuses (disperses) into the surrounding seawater it serves to directly reverse ocean acidification (i.e., by utilizing the base substance in the ocean alkalinity product to increase the ocean seawater's alkalinity), and indirectly reduces atmospheric CO2 (i.e., increasing the ocean seawater's alkalinity increases the ocean's ability to absorb/capture atmospheric CO2). Moreover, because the generated base substance is fully dissolved in the ocean alkalinity product, the electrochemical OAE approach avoids problems associated with other OAE approaches (e.g., dissolution kinetics issues that are associated with conventional mineral OAE approaches).\|[0011] Although electrochemical OAE approaches show great potential in mankind's efforts to combat global warming and ocean acidification, their widespread acceptance as a suitable NET may be predicated on the continued development of OAE system features that minimize cost per unit of captured/removed atmospheric CO2 (LCOC). For economic reasons related to carbon offsets and trading, NETs having relatively low LCOC ratings are typically favored over NETs exhibiting relatively high LCOCs. When calculating a NET's LCOC rating, many factors are taken into consideration, including capital costs (e.g., construction and installation expenses), and ongoing operating costs (e. g., land, water, maintenance, and electrical power expenses). In the case of OAE systems, the amount of atmospheric carbon removed from the atmosphere over an ocean depends on the amount of base substance supplied to the ocean (i.e., by way of the ocean alkalinity product), whereby the LCOC of an OAE system is predominantly determined by its levelized cost of producing each unit of base substance. In terms of the capital cost components of LCOC, OAE systems have an advantage over many NETs in that OAE systems are relatively inexpensive to construct and install, have a relatively small footprint and can be controlled using automated operating systems. Moreover, due to the high energy consumption and wear-related part replacement costs associated with performing the electrochemical salt-conversion process (described above), the most significant operating costs associated with an OAE system arise in the operation of the OAE system's BPED. Therefore, developments that reduce BPED operating costs arguably provide the most promising way to reduce OAE system LCOC.\|[0012] The BPEDs currently utilized in OAE systems are referred to herein as 3-chamber BPEDs for brevity. Such 3-chamber BPEDs may be characterized by utilizing an electrodialysis apparatus having an ion exchange (IE) stack configured in a 3-chamber cell arrangement, and by utilizing a flow control system capable of directing three different aqueous solutions (i.e., a salt feedstock solution, an acid solution, and a base solution) through corresponding salt/acid/base chambers of the IE stack. The IE stack includes multiple 3-chamber cells arranged in series between opposing electrodes, where each 3-chamber cell includes salt, acid and base chambers that respectively serve as parallel flow channels for the aqueous salt, acid and base solutions as they pass through the IE stack (i.e., each cell includes a salt chamber that channels a portion of the salt feedstock solution, an acid chamber that channels a portion of the aqueous acid solution, and a salt/base chamber that channels a portion of the base solution). Each cell's salt chamber is disposed between and separated from the cell's acid and salt/base chambers by corresponding ion exchange membranes, which are configured to facilitate the transfer of sodium and chloride ions from the salt chamber into the base and acid chambers during the electrochemical process. That is, during the electrochemical process an electric field applied across the IE stack by the electrodes produces an ionic current in a direction perpendicular to the parallel flow paths, whereby anions in the salt/base/acid streams (e.g., chloride ions (Cl−) and hydroxide ions (OH−)) move toward the positive electrode (anode) and cations in the salt/base/acid streams (e.g., sodium ions (Nat) and protons (H+)) move toward the positive electrode (anode). This ionic current causes dissociated salt molecules (i.e., sodium ions (Na+) and chloride ions (Cl−)) to exit the salt feedstock stream in opposite directions (i.e., such that the chloride ions (Cl−) pass through a first ion exchange filter from the cell's salt chamber into the cell's acid chamber, and the sodium ions (Nat) pass through a second ion exchange filter into the acid chamber). The chloride ions (Cl−) then combine with protons (H+) to form “new” acid (HCl) molecules in the acid solution stream passing through each cell's acid chamber, and the sodium ions (Nat) combine with hydroxide ions (OH−) to form “new” base (NaOH) molecules in the base solution stream passing through each cell's salt/base chamber. As a result of this electrochemical salt-conversion process, the base solution exiting the IE stack, which combines the base solution flows exiting each of the cells, has a significantly higher concentration of base substance (e.g., NaOH molecules) than before entering the IE stack. Similarly, the acid solution exiting each cell has a higher concentration of acid substance (e.g., HCl molecules) than before entering the IE stack. That is, the 3-chamber IE stack arrangement is configured such that three separate streams exit the ED apparatus: a reduced-salt solution stream (i.e., having a lower salt content than the salt feedstock solution fed into the ED apparatus), an acid product (strong acid) stream including the “new” acid molecules, and a base product (strong base) stream including the “new” base molecules.\|[0013] The main operational costs associated with 3-chamber BPEDs include the cost of externally supplied electricity and maintenance (e.g., replacement part and manual labor) associated with the IE stack, flow control system and other BPED subsystems required to perform the electrochemical salt-conversion process. A majority of the externally supplied electricity needed to power a given BPED operations is consumed by the IE stack (i.e., to generate the electric field that produces the ionic current) and varies in accordance with the BPED's IE stack arrangement. That is, larger capacity IE stacks (i.e., those capable of generating larger amounts of base substance per hour) typically require a larger number of series-connected cells. Although the salt/acid/base solutions are conductive, each ion exchange membranes functions like a resistor that impedes the applied electric field. Therefore, larger capacity IE stacks require larger amounts of externally supplied electricity to maintain an electric field at a suitably strong level across a larger number of cells (i.e., across a larger number of ion exchange membranes) than that required by smaller capacity IE stacks. Moreover, a significant amount is needed to power the flow control system (e.g., the various pumps and valves required to maintain the pressures and flow rates of the salt/acid/base solution streams) and other BPED subsystems, such as feedstock pretreatment units that are typically utilized to remove solids and other contaminants (e.g., divalent ions) from the aqueous salt feedstock solution (e.g., seawater) in order to reduce fouling (e.g., mineral scaling) in the IE stack. BPED maintenance costs include the cost of replacing parts that periodically wear out during normal BPED operations, costs associated with service/labor required to replace these parts, and costs associated with maintenance-related down-time (i.e., the periods of OAE system non-operation that are required to perform maintenance operations). Similar to the cost of externally supplied electricity, maintenance costs are typically higher for BPEDs with larger capacity IE stacks than BPEDs with lower capacity IE stacks due to the need to periodically replace a greater number of expensive ion exchange membranes and the higher expense associated with the replacement of flow control system and pretreatment unit components capable of the required higher flow capacities. Because the effectiveness of OAE systems as a NET is strongly dependent on minimizing LCOC (i.e., minimizing the levelized cost of producing base substance), and because the cost of externally supplied electricity and maintenance costs (e.g., the cost of ion exchange filters/membrane replacement) represent two of the most significant expenses associated with an OAE system's production of base substance, there is a strong motivation to optimize OAE system operations in a way that minimizes these two cost components.\|[0014] Enhanced ocean weathering (EOW) represents another promising ocean capture approach that both reduces atmospheric CO2 and mitigates ocean acidification. EOW involves spreading finely ground alkaline aggregate (e.g., silicate rock, such as basalt) onto large ocean surface areas. The widely dispersed alkaline aggregate captures large amounts of dissolved CO2 while in contact with the ocean water. The alkaline aggregate then sinks below the surface, thereby storing the captured CO2 in the ocean and slowing ocean acidification by way of direct interaction between the ocean's seawater and the alkaline material. A major challenge faced by EOW technologies is how to maximize CO2 drawdown for a given amount of finely ground alkaline aggregate. Currently, the best strategies for addressing this challenge at scale involve crushing/grinding the alkaline rock into extremely small particles and then dispersing these particles over large areas of the ocean to maximize the ratio of surface area to dispersed volume. A problem with these EOW strategies is that both the crushing/grinding and dispersing processes require a significant amount of energy. As explained above, the effectiveness of EOW systems as a NET is strongly dependent on minimizing LCOC, and because the cost of externally supplied electricity to crush/grind the alkaline rock represents one of the most significant expenses associated with an EOW system, there is a strong motivation to optimize EOW system operations in a way that minimizes this cost component.\|[0015] Seawater desalination is the process of removing salt and other contaminants from seawater, making it suitable for human consumption, irrigation, or industrial uses. Seawater desalination allows coastal communities to use a broader variety of water sources than conventional techniques, improving the resilience of water-stressed communities. Seawater desalination will become increasingly important as climate change threatens traditional water resources. As sea levels rise, existing freshwater aquifers for coastal communities are at an increasingly high risk of seawater intrusion, thereby making seawater desalination an important potential tool to help these communities adjust to climate change.\|[0016] Seawater desalination systems utilize either thermal technologies or membrane-based technologies. Thermal desalination systems heat seawater so that H2O evaporates into steam, leaving behind salt and other impurities, then condenses the steam back into liquid freshwater that is suitable for human consumption or other freshwater uses. Membrane-based desalination describes a class of technologies in which saline water passes through a semi-permeable material that allows H2O through but holds back dissolved solids like salts. Reverse osmosis is the most common membrane-based desalination technology that reverses the natural osmosis process (i.e., the natural movement of freshwater from an area of low salt concentration to an area of high salt concentration) by utilizing high-energy pumps to pressurize seawater located on a first side of a semi-permeable material such that passes through the membrane to generate freshwater (sometimes referred to as permeate) on the opposing (second) side of the membrane and leaving behind high-salt content brine (i.e., aqueous solution having a significantly higher salt content than that of seawater) on the first side of the membrane. Note that the pressure required to force freshwater through a membrane is directly proportional to the feedstock solution's salt content (i.e., saltier water having a relatively high salt concentration requires more pressure than less salty water), but this pressure is limited by the strength of the membrane (i.e., the membrane will rupture if the pressure is too high). Therefore, the strength of the membrane effectively creates an upper limit on the salinity of water that can be treated at a given flow volume, and a feedstock solution having a salt content much higher than seawater typically cannot be purified using reverse osmosis technologies.\|[0017] Problems associated with all seawater desalination technologies are related to the disposition of brine, high operating costs and carbon footprint. Both thermal and membrane-based desalination technologies generate brine having a higher salt concentration than seawater that is typically disposed of by supplying the brine into the ocean in a manner that both avoids ecological hazards (e.g., harm to sea life) and does not increase the salt content of the seawater feedstock drawn into the desalination plant (i.e., significant resources are required to disperse the brine over a large ocean region and far from the seawater feedstock input pipe). In addition, although the most efficient thermal desalination processes typically use more energy than membrane-based approaches, even reverse-osmosis seawater desalination consume large amounts of electrical energy (e.g., to drive seawater feed pumps and to achieve the pressures necessary to force permeate through semi-permeable membranes). This high energy consumption causes conventional seawater desalination plants to have both high operating costs and a large carbon footprint (i.e., due to the significant greenhouse gas emissions associated with the generation of the required electrical energy).\|[0018] What is needed is a system/method that reduces seawater desalination system operating costs (i.e., external electricity and/or maintenance) and greenhouse gas emissions while avoiding the ecological hazards and other problems associated with brine disposition. What is also needed is a carbon dioxide removal (CDR) system/method that minimizes LCOC by way of significantly reducing the operating costs associated with conventional EOAE systems/methods (i.e., external electricity and/or maintenance costs) and/or EOW systems/methods (i.e., crushing/grinding costs).\|SUMMARY OF INVENTION\|[0019] In an embodiment the present invention is directed to a modified desalination process and associated method that utilizes an electrochemical process to both mitigate the above-mentioned brine disposition problem and address other problems associated with conventional desalination systems/methods. Similar to conventional desalination processes, the modified desalination system/method is configured to convert a saltwater feedstock (e.g., brackish groundwater or seawater having an initial/first salt concentration) into a desired stream of freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a byproduct stream containing brine (i.e., saline solution having a relatively high (second) salt concentration that is higher than the initial salt content of the saltwater feedstock). According to an aspect, the modified electrochemical process is utilized to mitigate the above-mentioned brine disposition problem by effectively removing most of the salt from the brine stream in a way that effectively converts the brine stream into a reduced-salt stream having a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. According to another aspect, at least some of the reduced-salt stream generated by the electrochemical process is mixed/combined with the saltwater feedstock (i.e., such that the saltwater feedstock is effectively diluted by the reduced-salt stream before performing the desalination process), thereby reducing freshwater production costs by reducing the amount of salt that must be filtered/removed from the saltwater feedstock during the desalination process (i.e., in comparison to conventional processes in which only saltwater feedstock is desalinated).\|[0020] In an embodiment a modified desalination (or other) system includes an electrochemical reactor (e.g., a bipolar electrodialysis apparatus (BPED)), a mixing device and a desalination unit that are cooperatively coupled and configured to perform the modified desalination process mentioned above. The desalination unit utilizes known techniques to convert a saltwater feedstock having an initial (first) salt concentration into a freshwater stream and a brine stream having a relatively high (second) salt concentration, and the system is configured to direct (e.g., by way of pipes and pumps) the brine stream from an output terminal of the desalination unit to an input terminal of the electrochemical reactor. The electrochemical reactor is configured to channel three separate solutions: an aqueous salt solution that enters the reactor as the brine stream and exits as the reduced-salt stream, an aqueous acid solution that enters as a weak acid stream and exits as an acid product stream, and an aqueous base solution that enters as a weak base stream and exits as a base product stream. The electrochemical reactor is also configured to generate the reduced-salt stream by electrochemically processing the brine stream such that at least some of the salt molecules (e.g., NaCl) contained in the brine stream are converted into acid molecules (HCl) contained in the acid product stream and base molecules (NaOH) contained in a base product stream. According to another aspect, the electrochemical processing is performed at a rate that converts/removes a sufficient amount salt from the salt/saline solution such that the (third) salt concentration of the reduced-salt stream leaving the electrochemical reactor is lower than the initial (first) salt concentration of saltwater feedstock, thereby significantly reducing eco-safety risks and other brine disposition issues associated with conventional desalination systems/processes. According to another aspect, the system is further configured to direct (e.g., by way of pipes and pumps) at least some of the reduced-salt stream from the electrochemical reactor to an input terminal of the mixing device, which is configured to mix a saltwater feedstock stream (i.e., untreated feedstock or treated feedstock) with the reduced-salt stream received from the electrochemical reactor such that the resulting mixture stream has a (fourth) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock, and the desalination unit is configured to generate the freshwater stream and the brine stream by processing the mixture stream (desalination fluid) exiting the mixing device. Mixing (combining) the saltwater feedstock with the reduced-salt stream provides the system with two cost-saving benefits over conventional desalination systems: first, the energy cost required to produce each unit of freshwater is reduced because the amount of raw seawater or briny groundwater that must be pumped from a saltwater feedstock source to the desalination unit is reduced by an amount equal to that of the reduced-salt stream; and second, the operating/maintenance costs of the system are reduced by reducing the amount of salt that must be filtered or otherwise separated from the desalinated fluid (i.e., the feedstock/reduced-salt mixture) by the desalination unit. Accordingly, by utilizing an electrochemical reactor to remove salt from the brine stream generated by the desalination process, and then utilizing the reduced-salt stream generated by the electrochemical reactor to supplement/dilute the saltwater feedstock directed into the desalination unit, the modified desalination system both mitigates the above-mentioned brine disposition problem and addresses other problems associated with conventional desalination systems.\|[0021] In some embodiments, the system includes an optional pretreatment unit that is operably coupled between a saltwater feedstock source (e.g., ocean or well) and the mixing device, and is configured to remove solids and other contaminants from a stream (portion) of “raw” saltwater feedstock that has been pumped or otherwise delivered from the saltwater feedstock source (e.g., seawater pumped directly from an ocean or briny groundwater pumped from a well), and is further configured to deliver the resulting treated saltwater feedstock to the mixing device by way of the saltwater feedstock stream. In some embodiments the pretreatment unit includes filtering systems or other devices that function to remove solids and at least some contaminants (e.g., biological material and/or divalent ions) from the received raw saltwater feedstock. In an exemplary embodiment, the pretreatment unit includes one or more series connected filtering devices that utilize associated filters to remove contaminants from raw saltwater feedstock (e.g., a first filtering system that utilizes first filter(s) to remove solid particles from seawater, and a second filtering system that utilizes second filter(s) to selectively remove metals and/or biologic materials of value from the partially filtered seawater/brine received from the first filtering system). The filtered contaminants (e.g. removed solids, metals and/or biological materials) are removed from the feedstock flow path using known techniques, and the resulting treated (filtered) feedstock solution (i.e., the treated saltwater feedstock solution that has passed through the filters) forms the saltwater feedstock stream that is passed downstream to the mixing device for mixing with the reduced-salt stream received from the electrochemical reactor). In another exemplary embodiment, the pretreatment unit includes nanofiltration, ultrafiltration, chemical precipitation or other water purification system(s) that is/are configured to remove contaminants and reduce the hardness of the saltwater feedstock by filtering/removing dissolved metal ions and other hardness related minerals (e.g., calcium (Ca2+), magnesium (Mg2+), carbonate (CO3)2−, and iron (Fe2+/Fe3+)), and the system may be configured to return the filtered/removed hardness related minerals to the ocean by way of the ocean alkalinity product. Utilizing the pretreatment unit further reduces operating and maintenance costs by extending the uninterrupted operating period of the desalination unit. Moreover, because the reduced-salt stream is utilized as described above to reduce the required amount of raw saltwater feedstock, the cost of maintaining pretreatment units is lower than that of conventional desalination systems (i.e., reducing the amount of saltwater feedstock passed through the pretreatment unit reduces the rate of filter replacement or other periodic maintenance). In some embodiments a second ion removal process (e.g., filtering similar to that used to remove harness related minerals) is applied to the byproduct brine stream leaving the desalination unit (i.e., before the brine stream is supplied to the electrochemical reactor 110E), thereby further reducing operating costs. In other embodiments, the pretreatment unit may be omitted, for example, in cases where the raw saltwater feedstock is sufficiently free of contaminants when delivered to the desalination system.\|[0022] In some embodiments, the mixing device is configured to generate the mixture stream supplied to the desalination unit at a constant outflow rate by combining all of the reduced-salt stream received from the electrochemical reactor with a corresponding portion of the treated/untreated saltwater feedstock. As mentioned above, the salt content of the mixture stream exiting the mixing device is inversely proportional to the respective inflow rates of the reduced-salt stream and the saltwater feedstock, so minimizing the mixture stream's salt content (and thus minimizing desalination operating/maintenance costs) involves admitting as much of the reduced-salt stream as possible into the mixing device. In cases where the outflow rate of the mixture stream is determined by the combined reduced-salt stream and saltwater feedstock inflow rates, and is maintained constant (e.g., at the maximum processing rate of the desalination unit), the constant mixture stream outflow rate is achieved by admitting the total amount/inflow of the reduced-salt stream delivered to the mixing device and the controlling (i.e., increasing or decreasing) the saltwater feedstock inflow rate such that the combined inflow rates equal the constant mixture stream outflow rate. In some embodiments, a sensor monitors the flow rate of the reduced-salt stream delivered to the mixing device and a feedstock flow control device is utilized to control a (first) inflow rate of the saltwater feedstock stream into the mixing device, where the system controller controls the feedstock flow control device such that the (first) inflow rate is adjusted (increased/decreased) in accordance with changes (decreases/increases) in the (second) inflow rate of the reduced-salt stream into the mixing device. In some embodiments, the mixing device includes a mixing tank that receives the reduced-salt stream exiting the ED apparatus and a treated saltwater feedstock stream exiting a pretreatment unit such that the two streams intermix within the tank to form the mixture stream. In other embodiments, the mixing device may be implemented, for example, using interconnecting pipes or other mixing structures.\|[0023] As set forth above, the desalination unit functions to desalinate the mixture stream received from the mixing device to generate freshwater and the high-salt brine/feedstock stream. In some embodiments, the desalination unit utilizes a known desalination device/process (e.g., thermal desalination or membrane-based desalination) to separate the mixture stream into the desired freshwater (permeate) stream and the byproduct brine stream. In an exemplary embodiment, the desalination unit utilizes a reverse osmosis (RO) system including a semi-permeable membrane that prevents the passage of salt molecules, whereby the brine stream is formed on one side of the membrane and permeate (freshwater) passes to the opposing side of the membrane. Similar to conventional desalination processes, the freshwater generated by the desalination unit has a suitably low salt concentration (e. g., ≤500 ppm), and the brine stream comprises an aqueous solution having salt content greater than 50,000 ppm (5%).\|[0024] In an embodiment the electrochemical reactor is implemented using a bipolar electrodialysis system (BPED) of a type similar to that utilized in existing OAE systems to convert the high-salt brine stream into the reduced-salt stream. The BPED includes an electrodialysis (ED) apparatus that utilizes an ion exchange stack to perform an electrochemical salt-conversion process during which salt supplied in the brine stream is converted into a base substance and an acid substance. In some embodiments, the ion exchange stack comprising a series of salt chambers, acid chambers and base chambers that are arranged in series between opposing electrodes, where each salt chamber is located between and separated from associated pair of adjacent acid and base chambers by an associated intervening ion exchange membrane. The BPED also includes a flow control system including a first portion that is configured to direct the brine stream through the salt chambers of the ion exchange stack, a second portion configured to direct an aqueous acid solution through the acid chambers and a third portion configured to direct an aqueous base solution through the base chambers. During operation the opposing electrodes apply an electric field across the ion exchange stack to electrochemically process salt (e.g., NaCl) in the brine stream disposed in each salt chamber such that chlorine ions (Cl−) pass through first ion exchange membranes and combine with dissociated protons (H+) to form “new” acid molecules (HCl) in the aqueous acid solution disposed in the associated adjacent acid chamber, and such that sodium ions (Na+) pass through second ion exchange membranes and combine with dissociated hydroxide ions (OH−) to form “new” base molecules (NaOH) in the aqueous base solution disposed in the associated adjacent base chamber. In this manner, the electrochemical process causes the acid and base product streams leaving the ED apparatus to have a higher acid and base concentrations, respectively, than the acid/base solutions entering the ED apparatus. Conversely, the electrochemical process causes the reduction (removal) of salt from the brine solution passed through the ED apparatus, whereby the reduced-salt solution stream exiting the ED apparatus has a salt concentration that is substantially lower than that of the brine stream entering the ED apparatus. By utilizing a BPED similar to those used in stand-alone OAE systems (or another electrochemical reactor having a similar salt processing capacity), the reduced-salt solution can be generated with a salt concentration that is equal to or lower than that of seawater (e.g., below 35,000 ppm (3.5%)), thereby addressing the brine disposition issues associated with stand-alone desalination plants.\|[0025] In some embodiments, the electrochemical reactor also includes a fluid buffering system including an acid buffer tank and a base buffer tank that facilitate the circulation of the aqueous acid and base solutions through the ED apparatus. Specifically, the acid buffer tank is configured to contain the aqueous acid solution that is directed (by way of associated flow control elements) into the acid (second) chamber(s) of the ion exchange stack and to receive a first portion of the acid product stream exiting (directed away from) the acid chambers(s). Similarly, the base buffer tank is configured to contain the aqueous base solution that is directed to the base (third) chamber(s) of the ion exchange stack and to receive a first portion of the base product stream exiting the base chamber(s). Note that second portions of the acid and base product streams are typically diverted for other purposes (e. g., maintenance, OAE or commercial sale). As mentioned above, the electrochemical reactor's flow control system is configured such that the brine stream exiting the desalination unit is directed to the ED apparatus, and at least a portion of the reduced-salt stream exiting the ED apparatus is directed to the mixing device. This salt solution flow arrangement differs from BPEDs utilized in conventional OAE systems in which the reduced/depleted salt stream exiting an ED apparatus is typically utilized to replenish (make up) any acid/base product diverted from the electrochemical reactor for other purposes and to control the acid/base concentration (dilution) of the weak acid and base solutions directed to the ED apparatus. To facilitate dilution of the acid and/or solution streams in cases where all of the reduced-salt stream is directed to the mixing device, in one embodiment, the flow control system is further configured to divert some of the freshwater stream exiting the desalination unit such that it flows into the acid buffer tank and/or the base buffer tank. Although utilizing some of the freshwater for acid and/or base dilution reduces the amount of freshwater output from the system, the required dilution amount is typically much less than that produced by the desalination unit, and may provide a net benefit, for example, in cases where high quality acid product is desired (i.e., the acid product's value is typically inversely proportional to the amount of salt in the acid solution). In other embodiments, replenishing for the acid and/or base product streams may be achieved using a portion of the reduced-salt stream or using a mixture of both freshwater and reduced-salt streams.\|[0026] In some embodiments the brine stream exiting the desalination unit may be passed directly to the ED apparatus (i.e., the fluid buffer system may only include an acid buffer tank and a base buffer tank, and omit a salt buffer tank). In other embodiments, the fluid buffer system may include a salt buffer tank that is operably coupled between the desalination unit and the ED apparatus, and serves as a buffer for aqueous salt solution (i.e., such that a portion of the brine stream produced by the desalination unit is stored in the salt buffer tank). In this case, the salt buffer tank may be used to regulate the flow rate of brine into the ED apparatus.\|[0027] In some embodiments, the electrochemical reactor is configured to process brine at a rate that corresponds with a desired maximum freshwater production rate. That is, a desalination unit that is capable of generating freshwater at a relatively high flow rate also generates brine at a relatively high flow rate, so, to avoid the buildup of unprocessed brine, the electrochemical reactor must be capable of converting the brine stream into a corresponding reduced-salt stream at a corresponding flow rate. In addition to suitable flow control and buffer resources, the electrochemical reactor's ED apparatus must be configured to receive and process brine at the corresponding flow rate, for example, by way of providing a sufficient number of cells (i.e., groups of salt, acid and base chambers separated by intervening ion exchange membranes) arranged in series between suitable electrodes, and otherwise configuring the ED apparatus to facilitate the conversion of brine at the relatively high flow rate.\|[0028] In another exemplary embodiment, an integrated (combined) desalination/OAE system includes a seawater desalination subsystem and an OAE subsystem (electrochemical reactor). The seawater desalination subsystem generates a freshwater stream by desalinating seawater pumped or otherwise drawn from a nearby ocean using any of the desalination processes mentioned above. The OAE subsystem includes an ED apparatus that converts salt provided in the byproduct brine stream from the desalination process into acid and base product streams. The system also includes a post-production unit that selectively utilizes a portion of the base product stream to generate an ocean alkalinity product and selectively utilizes a portion of the acid product stream to generate an alkaline slurry, and then supplies (e.g., pumps) the ocean alkalinity product and the alkaline slurry to the ocean at a designated outfall location for OAE and enhanced ocean weathering (EOW) purposes (i.e., such that both the fully dissolved base substance in the ocean alkalinity product and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification). Integrating seawater desalination and at least one of OAE or EOW operations in the manner set forth herein essentially eliminates the ecological concerns associated with conventional stand-alone seawater desalination and significantly decreases total operating costs (i.e., in comparison with conventional stand-alone seawater desalination). That is, because the brine stream has a higher salt concentration than seawater, electrochemically processing the brine stream (i.e., in place of seawater) enhances the generation of ocean alkalinity product by decreasing the amount of externally supplied energy that is required to perform the electrochemical conversion of salt molecules (e.g., NaCl) into acid molecules (e.g., HCl) and base molecules (e.g., NaOH) for a given flow rate through the electrochemical reactor, thereby increasing the base product production efficiency and decreasing total operating cost over conventional stand-alone OAE systems that process seawater, thereby reducing LCOC in comparison to such OAE systems. Moreover, by generating and supplying alkaline ocean product and alkaline slurry to the ocean, the resulting OAE effectively offsets the carbon footprint of the seawater desalination process, and the integrated desalination/OAE system achieves greatly reduces total operating costs over separate (stand-alone) desalination and OAE plants. In addition, utilizing the reduced-salt stream, which is generated as a byproduct of the OAE process, to supplement the seawater (saltwater feedstock) processed by the desalination subsystem reduces operation and maintenance costs over conventional stand-alone seawater desalination plants, for example, by reducing the amount of raw seawater that must be pumped from an ocean and pretreated before desalination. Further, utilizing an electrochemical reactor to process the brine stream that is generated as a byproduct of the desalination process provides additional advantages including: (1) reducing environmental issues and dispersion costs associated with releasing high-salt-content brine directly from the desalination process into an ocean; and (2) reduces maintenance costs by facilitating the use of the generated acid product (e.g., HCl), e.g., to clean semi-permeable and/or ion exchange membranes utilized in the ion exchange stack. Moreover, integrating seawater desalination and OAE subsystems facilitates other benefits such as capital expense reductions achieved by shared plant facilities (e.g., project site and shelter/building), shared saltwater feedstock intake/outfall structures and associated operating costs, shared water treatment operating costs, and shared electrical infrastructure. Further, permitting (government authorization) for desalination plants is difficult in some regions because of eco-safety risks that are primarily due to the increased salinity of the outfall brine—the present invention mitigates this eco-safety risk by utilizing an electrochemical reactor to process the brine such that its final salinity is closer to ambient conditions, thereby leading to an easier permitting process for desalination plants modified in the manner described herein.\|[0029] Although described herein with specific reference to specific modified desalination and integrated desalination/OAE/EOW systems/methods, the present invention may also be utilized to provide other commercially advantageous operations that may achieve at least some of the benefits set forth above. For example, the base product and/or acid product generated by the electrochemical reactor/process may be selectively utilized for non-OAE uses. Although the carbon footprint of the resulting desalination system/process may be higher than that of the combined desalination/OAE approach, the desalination system/process would still have advantages over conventional seawater desalination operations. That is, utilizing the electrochemical reactor to reduce the salt content of the high-salt brine/feedstock stream significantly reduces eco-safety risks and other issues associated with the disposition of the high-salt brine generated by conventional desalination processes. In an exemplary embodiment, the system's controller may monitor one or more sites that provide input data including spot pricing for the base product and/or acid product generated by the electrochemical reactor. The controller may then utilize this input data to determine whether the base and/or acid products should be utilized for OAE/EOW purposes, or whether they should be sold to a third-party buyer. For example, when sufficient low/zero-carbon electricity is available from a power grid to offset the desalination process carbon footprint and the base product spot price is sufficiently high, then the controller may direct the post-production unit to divert the base product (e.g., some or all of the second base stream portion) for sale to a third-party buyer (i.e., instead of directing the base product to the ocean as part of ocean alkalinity product), whereby proceeds from the sale serve to reduce total operating costs of the system. Similarly, the control algorithm implemented by the system's controller may monitor input data from one or more sites that provide spot pricing for the acid product (e.g., HCl) generated by the electrochemical reactor, and utilizes this data to determine whether it is more cost effective to neutralize the acid product (e.g., by way of enhanced ocean weathering), or if selling the acid product may produce a greater value (i.e., if the acid product spot price is sufficiently high), in which case the controller may direct the post-production unit to divert the acid product (e.g., some or all of the second acid stream portion) for sale to a third-party buyer.\|[0030] According to another embodiment, a hybrid carbon dioxide removal (CDR) system includes an electrochemical OAE subsystem configured to generate an ocean alkalinity product, an EOW subsystem configured to generate an alkaline slurry, and a base delivery subsystem configured to supply at least one of the ocean alkalinity product and the alkaline slurry to an ocean to capture/reduce atmospheric carbon dioxide and mitigate ocean acidification. The electrochemical OAE subsystem utilizes an ED device configured to electrochemically process/convert salt into an acid substance and base substance and utilizes an alkaline product generator to generate an ocean alkalinity product including the base substance. In an exemplary embodiment, the EOW subsystem includes an accelerated ocean weathering reaction apparatus and a slurry generator. The accelerated ocean weathering reaction apparatus is configured to combine the acid substance from the electrodialysis device with an alkaline aggregate such that an accelerated ocean weathering reaction between the alkaline aggregate and the acid substance both neutralizes the acid substance and etches/weakens the alkaline aggregate. The slurry generator then receives the neutralized (fully processed) process fluid exiting the reaction apparatus and processes the etched/weakened alkaline aggregate into fine particles, thereby forming the alkaline slurry. In some embodiments, metal elements are released from the alkaline aggregate during the accelerated weathering and slurry generation processes and are reclaimed from the alkaline slurry to offset operating costs. The base delivery subsystem is configured to supply at least one of the ocean alkalinity product and the alkaline slurry to the ocean. By utilizing the acid substance of the electrochemical process to etch/weaken the alkaline aggregate, the accelerated (electrochemically assisted) ocean weathering process implemented by the EOW subsystem produces alkaline slurry at a significantly reduced cost in comparison to conventional EOW systems. That is, the acid substance, which is a byproduct of the electrochemical process and is therefore essentially cost free, serves to etch/weaken the alkaline aggregate, thereby increasing the etched/weakened aggregate's specific surface area and/or facilitating crushing/grinding the etched/weakened aggregate into alkaline particles suitable for ocean dispersal offsetting energy than would be required by conventional EOW crushing/grinding operations. Moreover, during the accelerated weathering operation the alkaline material in the alkaline aggregate neutralizes the acid substance, thereby circumventing acid storage/neutralization issues associated with conventional OAE technologies. Further, by supplying both the electrochemically generated ocean alkalinity product and the alkaline slurry to the ocean, the hybrid CDR system achieves at least the same amount of carbon capture removal and ocean deacidification as that achieved by independently operated conventional OAE and EOW systems using significantly less energy than separate conventional OAE and EOW systems. In some embodiments the CDR system utilizes a desalination subsystem to convert seawater from the ocean into a high-salt-content brine in order to enhance the electrochemical process.\|(US20250339810)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0031] FIG. 1 shows a modified desalination system according to an exemplary embodiment of the present invention;\|[0032] FIG. 2 shows a simplified electrochemical reactor that may be utilized to electrochemically process a brine solution in the modified desalination system of FIG. 1, according to an exemplary specific embodiment;\|[0033] FIG. 3 shows a simplified electrodialysis apparatus that may be utilized by the electrochemical reactor of FIG. 2 to electrochemically convert salt into acid and base products according to another exemplary embodiment;\|[0034] FIG. 4 shows a modified desalination system according to another exemplary embodiment; and\|[0035] FIG. 5 shows an integrated desalination/OAE/EOW system according to another exemplary embodiment of the present invention; and\|[0036] FIG. 6 shows an EOW subsystem of the integrated desalination/OAE/EOW system of FIG. 5 in additional detail according to an exemplary embodiment.\|(US20250339810)\|DETAILED DESCRIPTION\|[0037] The present invention combines desalination and electrochemical systems/processes in a way that converts a saltwater feedstock (e.g., seawater or briny groundwater) into freshwater suitable for human consumption and other freshwater uses, a base substance suitable for OAE purposes, and an acid substance. The invention is primarily described herein with specific reference to a modified desalination system/method that utilizes a desalination subsystem/process to convert saltwater feedstock into freshwater and brine and utilizes an electrochemical reactor/process to convert the brine into a reduced salt solution (i.e., by converting salt in the brine into acid and base substances). In one embodiment, the invention is described with reference to an integrated desalination/OAE/EOW system/method that desalinates seawater to produces freshwater and brine, electrochemically processes the brine to generate acid and base products, utilizes the base product to perform an OAE process, and utilizes the acid product to reduce the energy costs associated with crushing/grinding alkaline aggregate in an EOW process. However, in some embodiments, the systems/methods described herein may be utilized for other purposes, including a stand-alone hybrid HDR system/method or a system/method for generating acid and/or base substances in remote locations. The following description is presented to enable one of ordinary skill in the art to make and use the methods and systems described herein as provided in the context of specific embodiments. Various modifications to the embodiments will be apparent to those with skill in the art, and the general principles defined herein may be applied to other embodiments. Therefore, the methods and systems described herein are not intended to be limited to the particular embodiments shown and described, but are to be accorded the widest scope consistent with the principles and novel features herein disclosed.\|[0038] FIG. 1 depicts a modified desalination system 100 including an electrochemical reactor 110, a desalination subsystem 160 and a system controller 190. Electrochemical reactor 110 performs an electrochemical process in which a high-salt-content brine stream 111-1 is received from the desalination subsystem 160, salt contained in brine stream 111-1 is electrochemically processed (removed), and then at least a portion 111-21 of the resulting reduced-salt stream 111-2 is directed back to desalination subsystem 160. Desalination subsystem 160 performs a modified desalination process in which a mixing device 170 mixes (combines) a saltwater feedstock stream 51T (e.g., seawater or briny groundwater) with reduced-salt stream portion 111-21 received from electrochemical reactor 110 to form a mixture stream 51M, and then a desalination unit 180 processes (desalinates) mixture stream 51M to generate a freshwater stream 115 (i.e., water suitable for human consumption, irrigation, or industrial uses) and brine stream 111-1, which is directed to electrochemical reactor 110. System controller 190 controls the various operations performed by electrochemical reactor 110 and desalination subsystem 160 such that at least a portion of freshwater 115 exiting desalination subsystem 160 is directed out of system 100 as freshwater output stream 115-OUT for fresh water uses. Additional details regarding the various components and processes of system 100 are set forth below.\|[0039] Referring to the left side of FIG. 1, desalination subsystem 160 includes an optional pretreatment unit 165, a mixing device 170 and a desalination unit 180 that process saltwater feedstock 51 to generate freshwater stream 115 and brine stream 111-1.\|[0040] Optional pretreatment unit 165 is configured to treat a “raw” saltwater feedstock stream 51 (i.e., feedstock received directly from an external source, such as raw seawater pumped from an ocean 50, or briny groundwater pumped from a well) by removing (e.g., filtering) solids and other contaminants (e.g., biological material and/or divalent ions) from the raw feedstock. The resulting treated saltwater feedstock exiting pretreatment unit 165 is then supplied to mixing device 170 as saltwater feedstock stream 51T. Note that optional pretreatment unit 165 does not significantly reduce or otherwise change the salt content of the saltwater feedstock (i.e., the treated saltwater forming saltwater feedstock stream 51T has substantially the same initial (first) salt concentration as the raw saltwater forming feedstock stream 51. Pretreatment unit 165 may be omitted, for example, is cases where raw saltwater feedstock stream 51 is sufficiently pure (i.e., free of contaminants), or in embodiments where the raw saltwater feedstock is treated prior to being delivered into desalination subsystem 160. When pretreatment unit 165 is omitted, raw saltwater feedstock is passed directly to mixing device 170 (i.e., saltwater feedstock stream 51T and raw saltwater feedstock stream 51 comprise the same saltwater feedstock stream).\|[0041] Mixing device 170 is configured to receive reduced-salt stream portion 111-21 from electrochemical reactor 110 (i.e., some or all of reduced-salt stream 111-2 exiting ED apparatus 130) and saltwater feedstock stream 51T from pretreatment unit 165. Mixing device 170 utilizes one or more mechanisms (e.g., a mixing tank and/or pumps) to mix (combine) the two streams and to produce a mixture stream 51M including a mixture solution having a (fourth) salt concentration that is between the initial (first) salt concentration of saltwater feedstock stream 51T and an intermediate (third) salt concentration of the reduced-salt stream 111-21. As described in additional detail below, electrochemical reactor 110 is configured to generate reduced-salt stream 111-2 such that the intermediate (third) salt concentration is lower than the initial (first) salt concentration of saltwater feedstock stream 51T. Therefore, mixture stream 51M comprises an aqueous solution having a salt concentration that is lower than the initial salt concentration of the saltwater feedstock. An outlet of mixing device 170 is operably coupled to an inlet of desalination unit 180 such that mixture stream 51M is directed into desalination unit 180. In some embodiments (not shown), the mixing process performed by mixing device 170 may be implemented by either optional pretreatment unit 165 or desalination unit 180.\|[0042] In some embodiments mixing device 170 is configured to generate mixture stream 51M by combining all of reduced-salt stream 111-21 received from electrochemical reactor 110 with a corresponding portion of the treated/untreated saltwater feedstock included in saltwater feedstock stream 51T. That is, the flow rate of mixture stream 51M exiting mixing device 170 is substantially equal to a sum of the inflow rate of reduced-salt stream 111-21 received from electrochemical reactor 110 and the inflow rate of saltwater feedstock stream 51T. In this preferred embodiment, mixture stream 51M includes the total amount of reduced-salt stream 111-21 received from electrochemical reactor 110 and adjusts, if necessary, the inflow rate of saltwater feedstock stream 51T (e.g., by way of a feedstock flow control device 171). For example, assuming desalination unit 180 is configured to process mixture stream 51M at a total flow rate of 100 units per minute, if electrochemical reactor 110 provides reduced-salt stream 111-21 to mixing device 170 at an inflow rate of 30 units/min then the corresponding inflow rate of saltwater feedstock stream 51T is adjusted to equal 70 units/min, and if electrochemical reactor 110 subsequently provides reduced-salt stream 111-21 at an inflow rate of 35 units/min then the corresponding inflow rate of saltwater feedstock stream 51T is adjusted to 65 units/min. Utilizing all of the available reduced-salt stream 111-21 to generate mixture stream 51M minimizes the amount of salt that must be removed from mixture stream 51M by desalination unit 180 (i.e., by minimizing the proportion of saltwater feedstock to reduced-salt solution in mixture stream 51M). Note that variations in the inflow rate of reduced-salt stream 111-21 may occur for purposes of project wide optimization. For example, when acid production is valued higher than freshwater and base production, then freshwater stream portion 115-2 may be directed to acid buffer tank 121-2 (i.e., to increase the value of acid product stream 112-2 by minimizing salt content), whereby more of reduced-salt stream 111-2 may be directed to mixing device 170 as reduced-salt stream portion 111-21. In other cases it may be determined that freshwater and/or base production may be optimized when both freshwater stream portion 115-2 and reduced-salt stream 111-22 are simultaneously directed to acid buffer tank 121-2 and/or base buffer tank 121-3, where the system controller adjusts the fractions of the freshwater and reduced-salt streams to optimize the salt content in the acid and base solutions. In other embodiments, system optimization may be achieved by replenishing (making-up) for the acid product stream 112-22 and/or base product stream 113-22 using only reduced-salt stream portion 111-22 with the remainder of reduced-salt stream 111-2 being directed to mixing device 170 as reduced-salt stream portion 111-21. Whenever system optimization requires a corresponding change (increase/decrease) in the inflow rate of salt stream portion 111-21 to mixing device 170, the system controller makes a corresponding adjustment (decrease/increase) to the inflow rate of saltwater feedstock stream 51T so that the outflow rate of mixture stream 51M remains constant.\|[0043] Desalination unit 180 is configured to perform a desalination process on mixture stream 51M in a manner that generates high-salt brine stream 111-1, which is then directed to electrochemical reactor 130, and freshwater stream 115 comprising water having a salt concentration that is suitable for human consumption (e.g., less than or equal to 0.05% (≤500 ppm). By way of example, when the saltwater feedstock comprises seawater pumped from an ocean, saltwater feedstock stream 51/51T has a salt concentration of about 3.5%, the relatively high salt concentration of brine stream 111-1 may be greater than 5%. As described in additional detail below, in alternative embodiments desalination unit 180 may be implemented using a thermal desalination system, a reverse osmosis system or another membrane-based (or other) desalination system.\|[0044] Referring to the right side of FIG. 1, electrochemical reactor 110 includes a fluid buffering system 120, an electrochemical reactor 130 and a flow control system. As set forth in additional detail below, electrochemical reactor 110 is configured to generate reduced-salt stream 111-2 by electrochemically processing the brine stream 111-1 such that at least some of the salt molecules (e.g., NaCl) contained in brine stream 111-1 are converted into acid molecules (e.g., HCl) contained in an acid product stream 112-2 and base molecules (NaOH) contained in a base product stream 113-2, and such that the reduced-salt stream 111-2 exiting the electrochemical reactor 110 has a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. Note that electrochemical reactor 110 is greatly simplified for descriptive purposes, and that additional details regarding its construction and operation are provided below with reference to the exemplary embodiments depicted in FIGS. 2 to 5.\|[0045] Fluid buffering system 120 includes an acid buffer tank (ABT) 121-2 and a base buffer tank 121-3. Acid buffer tank 121-2 is configured to contain an aqueous acid solution that is circulated through reactor 130 by way of associated flow control structures (e.g., pipes and pumps) such that a relatively weak acid stream 112-1 is directed from acid buffer tank 121-2 to reactor 130 and at least a portion 112-21 of a relatively strong acid product stream 112-2 leaving reactor 130 is directed back to acid buffer tank 121-2. Base buffer tank 121-3 is configured to contain an aqueous base solution that is circulated through reactor 130 by way of associated flow control structures such that a relatively weak base stream 113-1 is directed from base buffer tank 121-3 to reactor 130 and at least a portion 113-21 of a relatively strong base product stream 113-2 leaving reactor 130 is directed back to base buffer tank 121-3. In some embodiments, the flow control system is further configured to direct a portion 115-2 of freshwater 115 into one or more of acid buffer tank 121-2 and base buffer tank 121-3 to dilute the weak solutions directed into reactor 130.\|[0046] ED apparatus 130 generally includes an ion exchange (IE) stack 135 that is disposed between two electrodes (i.e., anode 138+ and cathode 138−). IE stack 135 typically includes multiple cells arranged in series between electrodes 138+ and 138−, where each cell includes three chambers that respectively serve as parallel flow channels for the aqueous salt, acid and base solutions as they pass through IE stack 135. For brevity and clarity, only one cell of IE 135 is depicted in FIG. 1, which is made up of a salt chamber 131 that functions to channel a portion of the aqueous salt solution, an acid chamber 132 that channels a portion of the aqueous acid solution, and a base chamber 133 that channels a portion of the aqueous base solution. Each cell's salt chamber 131 is disposed between and separated from the cell's acid chamber 132 and base chamber 133 by corresponding ion exchange membranes 134-1 and 134-2, which are configured to facilitate the transfer of sodium and chloride ions from the salt chamber into the base and acid chambers during the electrochemical process as described below. ED apparatus 130 also includes manifold or other structures (not shown) that are configured to cooperate with the flow control resources of BPED 110 to direct the three different (i.e., a salt, acid and base) aqueous solutions through corresponding salt/acid/base chambers of IE stack 135. Specifically, the aqueous salt solution enters IE stack 135 as brine stream 111-1 that is divided and directed (e.g., by an input manifold, not shown) into the inlet of each cell's salt flow channel 131, and the aqueous salt solution exits the IE stack 135 by way of an outlet of each cell's salt flow channel 131 (and an outlet manifold, not shown) as reduced-salt stream 111-2. Similarly, the aqueous acid solution enters IE stack 135 as a weak acid stream 112-1 that is directed into the inlet of each cell's acid flow channel 132 and exits the IE stack 135 by way of an outlet of each cell's acid flow channel 132 as acid product stream 112-2. Finally, the aqueous base solution enters IE stack 135 as a weak base stream 113-1 that is directed into the inlet of each cell's base flow channel 133 and exits the IE stack 135 by way of an outlet of each cell's base flow channel 133 as base product stream 113-2.\|[0047] During the electrochemical process the three (salt, acid and base) aqueous solutions are directed through IE stack 135 along parallel flow paths (e.g., in the vertical direction) while a stack voltage VSTACK is applied to electrodes 138+ and 138−. When stack voltage VSTACK is sufficiently strong, the resulting electric field E produces an ionic current across IE stack 135 in a direction perpendicular to the parallel flow paths (e.g., in the horizontal direction). This ionic current causes dissociated salt molecules (i.e., sodium ions (Na+) and chloride ions (Cl−)) to exit brine stream 111-1 in opposite directions (i.e., such that the chloride ions (Cl−) pass through ion exchange filter 138-1 from salt chamber 131 into the acid chamber 132, and the sodium ions (Nat) pass through ion exchange filter 138-2 into base chamber 133). The chloride ions (Cl−) then combine with protons (H+) to form “new” acid molecules (HCl) in the acid solution stream flowing through acid chamber 132, and the sodium ions (Na+) combine with hydroxide ions (OH−) to form “new” base molecules (NaOH) in the base solution stream flowing through base chamber 133. As a result of this electrochemical salt-conversion process, base product stream 113-2 exits each cell's base chamber 133 with a significantly higher concentration of base molecules than weak base stream 113-1 (i.e., the aqueous base solution before it enters IE stack 135). Similarly, acid product stream 112-2 exiting each cell's acid chamber 132 has a higher concentration of acid molecules than that of weak acid stream 112-1. Note that, because salt is converted (consumed) to generate the acid and base molecules, reduced-salt stream 111-2 exiting each cell's salt chamber 131 has a lower salt concentration than inflowing brine stream 111-1.\|[0048] Referring to the lower left portion of FIG. 1, system controller 190 controls the various operations performed by electrochemical reactor 110 by way of operation/control signals 191, and controls the various operations performed by desalination subsystem 160 way of operation/control signals 192 such that at least a portion of the freshwater 115 exiting desalination unit 180 is directed out of system 100 as freshwater output stream 115-OUT. In an embodiment system controller 190 controls the operating state of ED apparatus 130 such that the above-described electrochemical process is performed at a rate that converts/removes a sufficient amount salt from brine stream 111-1 such that reduced-salt stream 111-2 leaving electrochemical reactor 110 has a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. In some embodiments system controller 190 controls a flow rate of mixture stream 51M into desalination unit 180 using sensor data from sensors configured to measure the flow rate of reduced-salt stream portion 111-21 (i.e., some or all of reduced-salt stream 111-2) from electrochemical reactor 110 into mixing device 170 and using a feedstock flow control device (e.g., pump or valve) to control the associated flow rate of saltwater feedstock stream 51T into mixing device 170. Note that, because the salt concentration of reduced-salt stream 111-2 is lower than the initial (first) salt concentration of saltwater feedstock 51/51T, any non-zero flow rate of reduced-salt stream portion 111-21 into mixing device 170 causes the solution forming mixture stream 51M to have a (fourth) salt concentration that is lower than the initial (first) salt concentration of saltwater feedstock 51/51T. Therefore, although operational and maintenance costs associated with desalination subsystem 160 may be reduced by way of directing all (i.e., the totality of) reduced-salt stream 111-2 from ED apparatus 130 to mixing device 170, beneficial reductions in total system operating costs may be achieved when reduced-salt stream portion 111-21 includes less than all of reduced-salt stream 111-2, and the remaining portion is redirected for other purposes (e.g., reduced-salt stream portion 111-22 may be used in place of or in combination with freshwater portion 115-2 to replenish (make-up) the acid and base solutions stored in buffer tanks 121-2 and 121-3). In some embodiments, system controller 190 is implemented using one or more processors configured to implement a software-based control algorithm that utilizes one of a proportional integral derivative, machine learning and/or artificial intelligence to coordinate the desalination and OAE processes (described below). In some embodiments, controller 190 controls the operations performed by electrochemical reactor 110 to perform additional functions described in co-owned U.S. Pat. No. 11,629,067, cited above.\|[0049] FIG. 2 shows a generalized bipolar electrodialysis (BPED) system (electrochemical reactor) 110A of a type similar to that utilized in some Ocean alkalinity enhancement (OAE) systems. BPED 110A generally includes a fluid buffering system 120A, an ED apparatus 130A, a flow control system 140A and a series of flow lines that are described in additional detail below. Additional details of BPED 110A are provided in U.S. Pat. No. 11,629,067, entitled “OCEAN ALKALINITY SYSTEM AND METHOD FOR CAPTURING ATMOSPHERIC CARBON DIOXIDE”, which is incorporated herein by reference in its entirety.\|[0050] Referring to the upper portion of FIG. 3, fluid buffering system 120A includes an optional salt buffer tank 121A-1 utilized to receive and store brine stream (salt solution) 111-1, an acid buffer tank 121A-2 utilized to store an acid solution 112A, and a base buffer tank 121A-3 utilized to store a base solution 113A. Each buffer tank 121A-1 to 121A-3 can be implemented using a standard 1000 L IBC caged tote tank, where salt buffer tank 121A-1 includes a plastic containment unit 122A-1 having an inflow port 123A-1 operably coupled to receive brine stream 111-1 and an outflow port 124A-1 operably coupled to salt chamber(s) 131 of ion exchange stack 135, acid buffer tank 121A-2 includes a plastic containment unit 122A-2 having an inflow port 123A-21 operably coupled to receive acid product stream portion 112A-21 and an outflow port 124A-2 operably coupled to acid chamber(s) 132 of ion exchange stack 135, and base buffer tank 121A-3 includes a plastic containment unit 122A-3 having an inflow port 123A-31 operably coupled to receive base product stream portion 113A-21 and an outflow port 124A-3 operably coupled to base chamber(s) 133 of ion exchange stack 135. Portions of freshwater output stream 115 generated by desalination unit 180 (shown in FIG. 1) and/or portions of reduced-salt stream 111A-2 may be directed to buffering system 120A and utilized to dilute and maintain acid solution 111A and base solution 113A at suitable levels within buffer tanks 121A-2 and 121A-3.\|[0051] Electrodialysis apparatus 130A includes ion exchange stack 135 and is otherwise configured and operates as described above with reference to FIG. 1 to electrochemical process NaCl (salt) molecules provided in brine stream 111-1 such that Cl-ions pass from salt chamber 131 though ion exchange membrane 134-1 into acid chamber 132 to enhance (i.e., decrease the pH of) acid solution 112A, and such that Nat ions pass from salt chamber 131 though ion exchange membrane 134-2 into base chamber 133 to enhance (i.e., increase the pH of) base solution 113A. Ion exchange stack 135 can be surrounded by a water-tight containment housing (not shown) to facilitate the flow of salt solution 111A through salt chamber(s) 131, the flow of acid solution 112A through acid chamber(s) 132, and the flow of base solution 113A through base chamber(s) 133. Cathode 138A− and anode 138A+ are disposed at opposite ends of ion exchange stack 135 and generate an electric field through the chambers in response to an applied voltage differential provided by a suitable voltage source VS, thereby electrochemically processing the salt, acid and base streams in the manner described herein.\|[0052] Similar to BPEDs utilized in OAE systems, flow control system 140A includes various control elements (e.g., pumps, valves etc.) that are collectively configured to direct streams of the acid and base solutions from buffer tanks 121A-2 and 121A-3 through corresponding chambers 132 and 133 of electrodialysis apparatus 130A and then back to buffer tanks 121A-2 to 121A-3 by way of associated conduits (flow lines). Specifically, weak acid stream 112A-1 exits acid buffer tank 121A-2 and is directed into acid chamber 132A by way of acid inflow line 1501A-2 and a pump 145A-21, and strong acid stream 112A-2 exits acid chamber 132A by way of acid outflow line 152A-2, with a first portion 112A-21 being returned to acid buffer tank 121A-2 by way of optional three-way valve 146A-2 and acid return line 153A-2, and a second portion 112A-22 of strong acid stream 112A-2 being diverted out of BPED 110A, e.g., for system maintenance purposes or commercial sale. Similarly, weak base stream 113A-1 exits base buffer tank 121A-3 and is directed into base chamber 133A by way of base inflow line 151A-3 and a pump 145A-31, a portion 113A-21 of strong base stream 113A-2 exiting base chamber 133A by way of base outflow line 152A-3 is returned to base buffer tank 121A-3 by way of three-way valve 146A-3 and a base return line 153A-3, and a second portion 113A-22 of strong base stream 113A-2 is diverted out of BPED 110A, e.g., for OAE purposes (e.g., as described below with reference to FIG. 5) or for commercial sale.\|[0053] BPED 110A differs from BPEDs typically utilized in OAE systems in that, unlike the acid and base solutions, flow control system 140A does not circulate all of weak salt solution exiting ion exchange stack 135 back to the acid/base buffer tanks. Instead, flow control system 140A is configured to direct brine stream 111-1 into salt chamber(s) 131 and to direct at least a portion 111A-21 of reduced-salt stream 111A-2 from salt chamber(s) 131 to mixing device 170 (shown in FIG. 1). Specifically, brine stream 111A-1 exits (flows from) salt buffer tank 121A-1 by way of outflow port 124A-1 and is directed into salt chamber 131 by way of salt inflow line 151A-1 and a first pump 145A-11, and reduced-salt stream 111A-2 exits salt chamber 131 by way of salt outflow line 152A-1. A valve 146A-1 is controlled by the system controller to direct a first portion 111A-21 of reduced-salt stream 111A-2 to mixing device 170 by way of an optional and an associated flow line 153A-1. A benefit of this arrangement is that, when ED apparatus 130A is operated such that reduced-salt stream 111A-2 has a salt concentration lower than that of the saltwater feedstock, less saltwater feedstock must be pumped to and processed by the desalination subsystem (not shown in FIG. 2), thereby reducing both operating energy and maintenance costs in at least some cases. Flow control system 140A also includes an optional valve 146A-4 that controllable by the system controller to direct a first portion 115-1 of freshwater stream 115 (received from desalination unit 180, see FIG. 1) for use as freshwater output stream 115-OUT, and directs second portion 115-2 of freshwater stream 115 to buffering system 120A (i.e., into one or both of acid buffer tank 121A-2 and base buffer tank 121A-3 to replenish acid/base product diverted from electrochemical reactor 110A for other purposes). Note that valve 146A-1 is also controllable to selectively direct a second portion 111A-22 of reduced-salt stream 111A-2 to fluid buffering system 120A for similar reasons.\|[0054] FIG. 3 shows a portion of a BPED system 110B including an ED apparatus 130B that includes an ion exchange stack 135B, an input manifold 136B-1, an output manifold 136B-2 and an electrolyte solution circulation system 139B. ED apparatus 130B may provide additional details regarding the multiple acid, salt and base chambers described above with reference to ED apparatus 130A (FIG. 2). That is, in some embodiments ED apparatus 130A (FIG. 3) is configured to include the features and details of ED apparatus 130B.\|[0055] Ion exchange stack 135B includes multiple acid chambers 131B-1 to 131B-N, multiple salt chambers 132B-1 to 132B-N and multiple base chambers 133B-1 to 133B-N disposed in a repeating series of cells that are arranged in series between two end chambers 137B-1 and 137B-2. For example, a first cell in the series may include salt chamber 131B-1 disposed between associated acid chamber 132B-1 and associated base chamber 133B-1, and a last cell in the series may include salt chamber 131B-N disposed between associated acid chamber 132B-N and associated base chamber 133B-N. Each of the acid, salt and base chambers of ion exchange stack 135B may function as described above with reference to acid chamber 132, salt chamber 131 and base chamber 133, respectively, to process a corresponding portion of one of the acid, salt and base solution streams directed through ion exchange stack 134B by way of input manifold 136B-1 and output manifold 136B-2. That is, input manifold 136B-1 may split weak acid stream 112B-1 (which is received from an acid buffer tank (not shown) by way of acid inflow line 151B-2) such that corresponding portions of the acid stream pass through each acid chamber 131B-1 to 131B-N. Similarly, input manifold 136B-1 receives brine stream 111-1 by way of salt inflow line 151B-1 and splits brine stream 111-1 into multiple stream portions that are directed through salt chambers 131B-1 to 131B-N, and receives weak base stream 113B-1 from a base buffer tank (not shown) by way of base inflow line 151B-3 and splits weak base stream 113B-1 into multiple stream portions that are directed through base chambers 133B-1 to 133B-N. End chambers 137B-1 and 137B-2 may function to conduct an electrolyte solution indicated by “ES” for purposes described below.\|[0056] Ion exchange stack 135B may include four types of ion permeable membranes that are respectively disposed between adjacent acid, salt, base and end chambers and facilitate the ion transfer process utilized to strengthen the base stream and the salt stream during operation of BPED 110B (i.e., when ion exchange stack 135B receives an electric field generated applying voltage potentials V+ and V− to anode 138B+ and cathode 138B−, respectively). The four types of membranes are indicated in FIG. 3 using the prefixes “A”, “K”, “B” and “F”, where membranes A1 to An are anion exchange membranes, membranes K1 to Kn are cation exchange membranes, membranes B1 to Bn are bipolar membranes, and membranes F1 and F2 are end membranes having characteristics described below. Electrolyte solution circulation system 139B may include a reservoir 139B-0 and flow lines 139B-1 to 139B-3 that function to circulate an electrolyte solution 114B through end chambers 137B-1 and 137B-2. That is, electrolyte solution 114B can be pumped from reservoir 139B-0 along first flow line 139B-1 to first end chamber 137B-1, from end chamber 137B-1 along second flow line 139B-2 to second end chamber 137B-2, and from second end chamber 137B-2 along third flow line 139B-3 to reservoir 139B-0. During operation the electrolyte solution may give up Na+ ions at one end of ion exchange stack 134B and reabsorbs Nat ions at the opposing end of ion exchange stack 135B. In some embodiments, electrolyte solution 114B is implemented using sodium sulfate or a semi conductive solution such as sodium hydroxide.\|[0057] FIG. 4 shows a modified desalination system 100D including an electrochemical reactor 110D and a desalination subsystem 160D.\|[0058] Referring to the lower portion of FIG. 4, electrochemical reactor 110D generally includes a fluid buffering system 120D, an ED apparatus 130D and a flow control system 140D. Fluid buffering system 120D includes an acid buffer tank (ABT) 121D-2 and a base buffer tank (BBT) 121D-3. Acid buffer tank 121D-2 stores an aqueous acid solution formed by a portion 112D-21 of an acid product stream 112D-2 exiting ED apparatus 130D and a portion 115D-21 of freshwater stream 115D exiting desalination subsystem 160D and supplies a relatively weak acid stream 112D-1 to ED apparatus 130D. Base buffer tank 121D-3 stores an aqueous base solution formed by a portion 113D-21 of a base product stream 113D-2 exiting ED apparatus 130D and a portion 115D-22 of freshwater stream 115D exiting desalination subsystem 160D and supplies a relatively weak base stream 113D-1 to ED apparatus 130D. ED apparatus 130D includes an ion exchange stack 135D disposed between electrodes 138D− and 138D+, an input manifold 136D-1 and an output manifold 136D-2, and is configured to receive and electrochemically process brine stream 111D-1, weak acid stream 112D-1 and weak base stream 113D-1 in the manner described above to generate reduced-salt stream 111D-2, acid product stream 112D-2 and base product stream 113D-2. Flow control system 140D includes pipes, pumps (indicated by circled arrows) and valves that are configured to direct the various solution flows between desalination subsystem 160D and electrochemical reactor 110D, and to selectively divert a portion 113D-22 of base product stream 113D-2 and a portion 112D-22 of acid product stream 112D-2 for one or more non-OAE purposes (e.g., for sale to a third party, or for system maintenance or commercial purposes). Flow control system 140D also includes flow control valves 146D-1 and 146D-4. Flow control valve 146D-1 effectively divides freshwater 115D exiting RO unit 180D into a first freshwater stream portion 115D-1 that is directed out of system 100D as freshwater output stream 115D-OUT and a second freshwater stream portion 115D-2 directed to fluid buffering system 120D. Flow control valve 146D-4 effectively divides reduced-salt stream 111D-2 into a first reduced-salt stream portion 111D-21 directed to desalination subsystem 160D and a second reduced-salt stream portion 111D-22 directed to fluid buffering system 120D. As discussed below, the system controller may utilize sensors and other control data to determine the flow amounts (flow rates) of each stream portion 111D-21, 111D-22, 115D-1 and 115D-2, and to adjust the operating states of flow control valves 146D-1 and 146D-4 by way of appropriate control signals to achieve the determined flow amounts.\|[0059] Referring to the upper portion of FIG. 4, desalination subsystem 160D includes a pretreatment unit 165D, a mixing tank (mixing device) 170D and a reverse osmosis system (desalination unit) 180D.\|[0060] Pretreatment unit 165D includes a solids filtering device 166D and a metals/biological removal device 168D that are connected in series such that raw saltwater feedstock 51 must pass through both series-connected filtering devices before being supplied to mixing tank 170D. Each filtering device 166D and 168D utilizes an associated filter to remove targeted contaminants from raw saltwater feedstock 51 (e.g., filtering system 166D utilizes one or more filters 167D that are optimize to remove solid particles from feedstock 51, and filtering system 168D utilizes one or more filters 169D that are optimized to remove metals and/or biologic materials from partially filtered seawater/brine 51T1 received from the first filtering system 166D). The order and number of filtering devices may be different from that shown in FIG. 4. As indicated by the arrows in the upper right portion of FIG. 4, the filtered contaminants (e.g. removed solids, metals and/or biological materials) are removed from the feedstock flow path using known techniques, and the resulting treated (filtered) feedstock solution 51T2 (i.e., the treated saltwater feedstock solution that has passed through both filters 167D and 169D) forms a treated saltwater feedstock stream 51T2 that is passed downstream to mixing tank 170D.\|[0061] Mixing tank 170D is configured to receive reduced-salt stream portion 111D-21 (i.e., some or all of reduced-salt stream 111D-2 exiting ED apparatus 130D) and treated saltwater feedstock stream 51T2 from pretreatment unit 165D. Mixing tank 170D is also configured such that treated saltwater 51T and reduced-salt stream 111D-2 combine (intermix) within the mixing tank 165D to form saltwater/reduced-salt mixture 51M, which is then passed to RO system 180D. Mixing tank 170D is configured to generate mixture stream 51M by combining all of reduced-salt stream portion 111-21 received from electrochemical reactor 110 with a corresponding portion of treated/untreated saltwater feedstock 51T2, which may be controlled by way of a feedstock flow control device 171D in a manner similar to that described above with reference to FIG. 1.\|[0062] RO system 180D receives mixtures stream 51M from mixing tank 170D and utilizes a semi-permeable membrane 181D that prevents the passage of salt molecules, whereby brine stream 111D-1 is formed on one side of membrane 181D and permeate (freshwater) passes through membrane 181D and exit as freshwater stream 115D. Similar to conventional desalination processes, freshwater stream 115D generated RO unit 180D has a suitably low salt concentration (e.g., ≤500 ppm), and brine stream 111-1 comprises an aqueous solution having salt content greater than 50,000 ppm (5%), whereby at least a portion of freshwater stream 115D is suitable for use as freshwater output stream 115D-OUT (i.e., suitable for human consumption and other freshwater uses).\|[0063] Modified desalination system 100D also includes a system controller (not shown) that controls the various operations performed by electrochemical reactor 110D and desalination subsystem 160D way of operation/control signals in the manner described above. In addition, the system controller controls the operating states of flow control valves 146D-1 and 146D-4 in response to sensor data and/or externally supplied data to optimize system operations for reasons set forth above. In some embodiments, flow control valve 146D-4 may be controlled to stop all flow of reduced-salt solution to mixing device 170D, for example, when insufficient clean energy is available and/or electrochemical reactor 110D is shut down. During such periods system 100D may be operated in a manner similar to that implemented by a conventional desalination system.\|[0064] FIG. 5 depicts a system 100E according to another embodiment. In the depicted embodiment, system 100E includes an OAE subsystem (electrochemical reactor) 110E, a seawater desalination subsystem 160E and an enhanced ocean weathering (EOW) subsystem 200, whereby system 100E is sometimes referred to herein as an integrated desalination/OAE/EOW system. However, in some embodiments EOW subsystem 200 may be omitted, whereby system 100E may be referred to as an integrated desalination/OAE system (i.e., by way of including OAE subsystem 110E and seawater desalination subsystem 160E). In other embodiments, seawater desalination subsystem 160E may be omitted (e.g., seawater 51 is pumped directly to OAE subsystem 110E), whereby system 100E may be referred to as a hybrid CDR system for reasons that will become clear below. Therefore, although system 100E is depicted as an integrated desalination/OAE/EOW system, it is understood that FIG. 5 also shows an integrated desalination/OAE system and a hybrid CDR system.\|[0065] Referring to seawater desalination subsystem 160E (lower portion of FIG. 5), seawater 51 is pumped or otherwise drawn from ocean 50 into a pretreatment unit 165E (e.g., a nanofiltration, ultrafiltration, chemical precipitation or other water purification system) that is configured to treat (i.e., remove contaminants from) seawater 51. Treated seawater 51T is then mixed with reduced-salt stream 111E-22 in mixing device 170E to form a treated seawater/reduced-salt mixture solution 51M, and then mixture solution 51M is processed by a desalination unit 180E (e.g., a membrane-based or thermal desalination system) to generate freshwater 115E and a byproduct brine stream 111E-1, thereby providing freshwater output stream 115E. In one embodiment, pretreatment unit 165E is configured to remove hardness related minerals HRM (along with other contaminants) such that a hardness of seawater 51 is reduced before being supplied to mixing device 170E. In some embodiments, as indicated by the dashed-line arrow, the hardness related minerals HRM are supplied to a post-production unit 150E and returned to ocean 50 with the ocean alkalinity product and/or alkaline slurry (both discussed below).\|[0066] OAE subsystem 110E includes a fluid buffering system 120E, an ED apparatus 130E and a flow control system that are configured and operate in the manner described in at least one of the previously described embodiments. ED apparatus 130E converts salt provided in brine stream 111E-1 into acid molecules (e.g., HCl) disposed in an acid product stream 112E-2 and base molecules (e.g., NaOH) disposed in a base product stream 113E-2. Base buffer tank 120E includes an acid buffer tank (ABT) that receives a (first) portion 112E-21 of acid product stream 112E-2 and supplies a weak acid stream to ED apparatus 130E, a base buffer tank (BBT) that receives a (first) portion 113E-21 of base product stream 113E-2 and supplies a weak base stream to ED apparatus 130E, and an optional salt buffer tank (SBT) that receives brine stream 111E-1 from desalination unit 180E and supplied brine stream 111E-1 to ED apparatus 130E. Although not depicted in FIG. 5 for clarity, portions of reduced salt stream 111E-2 and/or freshwater stream 115E may be directed to acid buffer tank (ABT) and base buffer tank (BBT) for the make-up and dilution purposes discussed above.\|[0067] System 100E also includes a post-production unit 150E that selectively utilizes a portion 113E-22 of base product stream 113E-2 to generate an ocean alkalinity product 113E-OUT and selectively utilizes a portion 112E-22 of the acid product stream 112E-2 to generate an alkaline slurry 246, and then supplies (e.g., pumps) the ocean alkalinity product 113E-OUT and the alkaline slurry 246 to the ocean 50 at a designated outfall location 50-1 for OAE purposes (i.e., such that both the fully dissolved base substance in the ocean alkalinity product and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide CO2 and mitigate ocean acidification). In the exemplary embodiment, a portion of post-production unit 150E that is considered part of OAE subsystem 100E includes an acid product tank 127E-2, a base product tank 127E-3, an alkalinity product (ALK PROD) generator 153E and a base delivery subsystem 159E. Acid product tank 127E-2 receives and stores a portion 112E-22 of acid product stream 112E-2, and base product tank 127E-3 receives and stores a portion 113E-22 of base product stream 113E-2. Alkalinity product generation unit 153E is configured to generate an ocean alkalinity product 113E-OUT using a base product stream portion 113E-31, which is received from base product tank 127E-3, such that ocean alkalinity product 113E-OUT includes base molecules (NaOH) that are fully dissolved in a salt solution and has a pH level that is a predetermined amount higher than a pH level of the ocean's seawater 51 (e.g., in a target pH range between 8.0 and 9). In some embodiments, the ocean alkalinity product 113E-OUT is generated using a dilution apparatus configured to operate in the manner described in co-owned and co-pending U.S. Published Patent Application No. US 2024-0336503 A1, entitled “PRODUCTION EFFICIENCY OPTIMIZATION FOR BIPOLAR ELECTRODIALYSIS DEVICE”, which was published on Oct. 10, 2024, and is incorporated herein by reference in its entirety. Post-production unit 150E also includes an enhanced ocean weathering (EOW) subsystem 200 that is configured to generate an alkaline slurry 246 using an acid product stream portion 112E-31, which is received from acid product tank 127E-2, by combining acid product stream portion 112-31 with a coarsely-ground alkaline aggregate (rock) such that a reaction between the alkaline aggregate and the acid molecule both neutralizes the acid molecules and etches/weakens the alkaline aggregate. Enhanced ocean weathering subsystem 200 is described in additional detail below with reference to FIG. 6. Base delivery subsystem 159E is configured and controlled by system controller 190E to supply (e.g., pump) at least one of ocean alkalinity product 113E-OUT and alkaline slurry 246 to ocean 50 at a designated outfall location 50-1.\|[0068] System controller 190E is programmed and otherwise configured to control operations of OAE subsystem 110E by way of control signals 191E, to control operations of desalination subsystem 160E by way of control signals 192E, and configured to control operations of post-production unit 150E by way of control signals 193E and 194E such that one or both of alkalinity product 113E-OUT and alkaline slurry 246 are selectively supplied to ocean 50 in safe and efficient manner. In one embodiment, system controller 190E monitors sensors and other data sources (e.g., via data 195E) and controls base delivery system 159E by way of control signal 194E such that ocean alkalinity product 113E-OUT and alkaline slurry 246 are only supplied to ocean 50 when data 195E indicates that sea life adjacent to outfall location 50-1 will not be endangered by the release of these OAE substances. In another embodiment, system controller 190E may monitor one or more sites that provide input data 195E including spot pricing for the base product and/or acid product generated by electrochemical reactor 110E. Controller 190E may then utilize this input data to determine whether the base and/or acid products should be utilized for OAE/EOW purposes, or whether they should be sold to a third-party buyer. For example, when sufficient low/zero-carbon electricity is available from a power grid to offset the desalination process carbon footprint and the base product spot price is sufficiently high, then the controller 190E may direct the post-production unit 150E (e.g., by way of control signals 191E) to divert a base product portion 113E-220 (e.g., some or all of the second base stream portion 113E-22) for sale to a third-party buyer (i.e., instead of directing the base product to ocean 50 as part of ocean alkalinity product 113E-OUT), whereby proceeds from the sale serve to reduce total operating costs of system 100E. Similarly, the control algorithm implemented by system controller 190E may monitor input data 195E from one or more sites that provide spot pricing for the acid product (e.g., HCl), and utilizes this data to determine whether it is more cost effective to neutralize the acid product (e.g., by way of EOW subsystem 200), or if selling the acid product may produce a greater value (i.e., if the acid product spot price is sufficiently high), in which case the controller 190E may direct the post-production unit 150E to divert an acid product portion 112E-220 (e.g., some or all of the second acid stream portion 112E-22) for sale to a third-party buyer.\|[0069] FIG. 6 shows EOW subsystem 200 of integrated desalination/OAE/EOW system 100E (see FIG. 5) according to an exemplary embodiment. EOW subsystem 200 includes an accelerated ocean weathering reaction apparatus 210, a dosing apparatus 230, a slurry generator 240 and a neutralization controller 280. Accelerated ocean weathering reaction apparatus 210 includes a reaction tank 211 configured to contain a process fluid 215 including a mixture of alkaline aggregate 95 and acid product portion 112E-31 until the acid molecules are neutralized and alkaline aggregate 95 is etched/weakened. In some embodiments, alkaline aggregate 95 may be transported from a quarry or other source by a material delivery vehicle 92 and processed by an optional pre-crusher/grinder 201 before the pre-crushed/ground alkaline aggregate 95-1 is delivered into reaction tank 211 by way of an inlet pipe 203. Dosing apparatus includes one or more dosing pumps 231 that receive acid product portion 112E-31 from acid product tank 127E-2 and is controlled by neutralization controller 280 to inject acid product doses 112E-4 into reaction tank 211 by way of an injector 235. Neutralization controller 280 controls the delivery/injection of alkaline aggregate and acid product into reaction tank 211 by way of monitoring a process fluid pH measurement data pHPF generated by a first sensor S1 disposed inside reaction tank 211 and acid product pH measurement data pHAP generated by a second sensor S2 disposed upstream from acid dosing pump(s) 231. During operation neutralization controller 280 controls the injection rate of acid product doses 112E-4 into reaction tank 211 such that a pH level of process fluid 215 is optimized such that acid molecules are neutralized and alkaline aggregate 95 is etched/weakened at a maximum rate. Neutralized product (i.e., a combination of neutralized acid solution and weakened/etched alkaline aggregate) is passed from reaction tank 211 to slurry generator 240 by way of an outlet pipe 241. Slurry generator 240 is configured to generate alkaline slurry 246 by processing (e.g., crushing/grinding) the etched/weakened alkaline aggregate of neutralized product 215N into fine particles, and then passes alkaline slurry 246 to base delivery subsystem 159E (see FIG. 5). In some embodiments, the accelerated weathering reaction causes the release of one or more metal elements (e.g., Nickel, Cobalt, Aluminum, Magnesium, Potassium and/or Lithium) from the alkaline aggregate and the slurry generator 240 is configured reclaim (i.e., separate and remove) the released metal elements from alkaline slurry 246 using known techniques, whereby system costs may be further reduced/offset by way of commercial sale of the reclaimed metals. In some embodiments, the operation of EOW subsystem 200 is controlled by system controller 190E by way of control signals 193E passed to neutralization controller 280.\|[0070] Referring again to FIG. 5, by configuring post-production unit 150E to implement both alkaline production generator 153E and EOW subsystem 200, system 100E implements a hybrid carbon dioxide removal (CDR) process and a reduced ocean acidification (ROA) process that combines some portions of each of a conventional electrochemical ocean alkalinity enhancement (EOAE) process and a conventional EOW process to achieve combined beneficial results (i.e., CDR/ROA-EOAE and CDR/ROA-EOW) achieved by both conventional processes, but changes other portions of each conventional processes in a way that reduces total operating costs (i.e., in comparison to separately performing the two conventional processes). For example, in one embodiment the hybrid CDR system implements the conventional EOAE process portions related to electrochemically processing salt to generate a base substance (e.g., NaOH) and an acid substance (e.g., HCl) and supplying the base substance to the ocean by way of an ocean alkalinity product, and the hybrid CDR system also implements the conventional EOW process portion related to mining and transporting alkaline aggregate/rock. The changes to the conventional EOAE and EOW processes occur after the acid byproduct is produced and after the alkaline rock is transported, whereby the conventional disposal of the acid byproduct and conventional crushing/grinding of the alkaline rock are replaced with an advanced weathering operation that includes combining alkaline rock and the acid product/substance generated by ED apparatus 130. In the embodiment described above with reference to FIG. 6, the advanced weathering operation involves mixing the acid product portion 112E-31 and alkaline rock/aggregate (e.g., olivine/basalt or other mafics/ultramafics) to produce alkaline slurry 246 with a pH between two and eight. As discussed above, slurry generation may include pre-grinding/crushing and/or post-reaction processing of the alkaline rock, but these optional processes require substantially less externally supplied energy than that required by the conventional crushing/grinding process and therefore costs less to perform than conventional acid disposal and crushing/grinding. During the advanced weathering operation, the acid substance in the acid byproduct reacts with alkaline substances in the alkaline rock, thereby weakening and/or increasing the surface area of the alkaline rock and neutralizing the acid substance. During the advanced weathering operation valuable and/or toxic metal constituents of the alkaline aggregate (Ni, Co, Al, Mg, K, Li, etc.) may be reclaimed from the slurry using known techniques. The advanced weathering process proceeds until the acid substance (e.g., HCl) supplied in the acid byproduct is neutralized, at which point the final alkaline slurry has a pH higher than ambient ocean pH (>7.5). The final alkaline slurry could then be dispersed into the ocean via fixed point (e.g., by way of base delivery subsystem 159E) or released from a moving vessel.\|[0071] Although the invention is primarily described herein in the context of seawater desalination and seawater-based OAE systems/methods, various novel aspects described herein may be beneficially utilized in other systems/methods without departing from the spirit and scope of the invention. For example, the chemical reactor implemented by the present invention may be utilized to electrochemically process a wide variety of salt types to generate corresponding base and acid substances. It will be clear to those skilled in the art that the inventive features of the present invention are applicable to these other embodiments as well, and that all of which are intended to fall within the scope of the present invention.	(US20250339810)\|RELATED APPLICATIONS/PATENTS\|[0001] This application claims priority from U.S. Provisional Patent Application No. 63/716,029, entitled “Integrated Ocean Alkalinity Enhancement And Seawater Desalination”, filed on Nov. 4, 2024, which is entirely incorporated herein by reference.\|[0002] This application also claims priority from U.S. Provisional Patent Application No. 63/641,910, entitled “Electrochemical Assisted Ocean Weathering”, filed on May 2, 2024, which is entirely incorporated herein by reference.\|(US20250339810)\|FIELD OF THE INVENTION\|[0003] The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|BACKGROUND\|[0004] As humans burn more and more fossil fuels, the resulting increased carbon dioxide (CO2) concentration in Earth's atmosphere causes both climate change and ocean acidification. The increased atmospheric concentrations of CO2 and other greenhouse gases (e.g., methane) produces climate change by trapping heat close to earth's surface, thereby increasing both air and sea temperatures. Because earth's oceans absorb about 25% of atmospheric CO2, and because the absorbed CO2 dissolves to form carbonic acid that remains trapped in the seawater, the increased atmospheric CO2 concentration caused by burning fossil fuels also produces ocean acidification by way of increasing the amount of CO2 gas dissolved in the ocean.\|[0005] Both climate change and ocean acidification pose Climate change in the form significant threats to humans. of increased global average temperatures can produce several dangerous effects such as the loss of polar ice and corresponding increased sea levels, disease, wildfires and stronger storms and hurricanes. Ocean acidification changes the ocean chemistry that most marine organisms rely on. One concern with ocean acidification is that the decreased seawater pH can lead to the decreased survival of shellfish and other aquatic life having calcium carbonate shells, as well as some other physiological challenges for marine organisms.\|[0006] To avoid dangerous climate change, the international Paris Agreement aims to limit the increase in global average temperature to no more than 1.5° C. to 2° C. above the temperatures of the pre-industrial era. Global average temperatures have already increased by between 0.8° C. and 1.2° C. The Intergovernmental Panel on Climate Change (IPCC) estimates that a ‘carbon budget’ of about 500 GtCO2 (billion tons of carbon dioxide), which corresponds to about ten years at current emission rates, provides a 66% chance of limiting climate change to 1.5° C.\|[0007] In addition to cutting CO2 emissions by curtailing the use of fossil fuels, climate models predict that a significant deployment of Negative Emissions Technologies (NETs) will be needed to avoid catastrophic ocean acidification and global warming beyond 1.5° C. (see “Biophysical and economic limits to negative CO2 emissions”, Smith P. et al., Nat. Clim. Chang. 2016; 6:42-50). Current atmospheric CO2 and other greenhouse gas concentrations are already at dangerous levels, so even a drastic reduction in greenhouse gas emissions would merely curtail further increases, not reduce atmospheric greenhouse gas concentrations to safe levels. Moreover, the reduction or elimination of certain greenhouse gas sources (e.g., emissions from long-distance airliners) would be extremely disruptive and/or expensive and are therefore unlikely to occur soon.\|[0008] Therefore, there is a need to supplement emission reductions with the deployment of NETs, which are systems/processes that serve to reduce existing atmospheric greenhouse gas concentrations by, for example, capturing/removing CO2 from the air and sequestering it for at least 1,000 years. The need for NETs may be explained using a bathtub analogy in which atmospheric CO2 is represented by water contained in a bathtub, ongoing CO2 emissions are represented by water flowing into the tub, and NETs are represented by processes that control water outflow through the tub's drain. In this analogy, reduced CO2 emission rates are represented by partially turning off the water inflow tap—the slower inflow rate provides more time before the tub fills, but the tub's water level will continue to rise and eventually overflow. Using this analogy, although reducing CO2 emissions may slow the increase of greenhouse gas in the atmosphere, critical concentration levels will eventually be reached unless NETs are implemented that can offset the reduced CO2 emission level (i.e., remove atmospheric CO2 at the same rate it is being emitted). Moreover, because greenhouse gas concentrations are already at dangerous levels (i.e., the tub is already dangerously full), there is an urgent need for NETs that are capable of significantly reducing atmospheric CO2 faster than it is being emitted to achieve safe atmospheric concentration levels (i.e., outflow from the tub's drain must be greater than the reduced inflow from the tap to reduce the tub's water to a safe level).\|[0009] NETs can be broadly characterized as Direct Air Capture (DAC) approaches and Ocean Capture approaches. DAC approaches utilize natural (e.g., reforestation) and technology-based methods to extract CO2 directly from the atmosphere. Ocean capture approaches utilize various natural and/or technological processes to remove CO2 from the atmosphere and store it in the ocean as bicarbonate, a form of carbon storage that is stable for over 10,000 years.\|[0010] Electrochemical ocean alkalinity enhancement (electrochemical OAE or EOAE) represents an especially promising ocean capture approach that both reduces atmospheric CO2 and mitigates ocean acidification by generating an ocean alkalinity product (i.e., an aqueous alkaline solution containing a fully dissolved base substance) and supplying the ocean alkalinity product to ocean seawater at a designated outfall location. Electrochemical OAE systems typically generate the required base substance using an electrochemical reactor referred to as a bipolar electrodialysis device (BPED), which generally includes an electrodialysis (ED) apparatus and associated flow control devices configured to perform an electrochemical salt-conversion process that converts salt supplied in an aqueous salt feedstock solution (e.g., seawater) into the base substance and an acid substance. The base substance produced by the BPED is then incorporated into the ocean alkalinity (base) product that is then supplied to the ocean. As the base substance diffuses (disperses) into the surrounding seawater it serves to directly reverse ocean acidification (i.e., by utilizing the base substance in the ocean alkalinity product to increase the ocean seawater's alkalinity), and indirectly reduces atmospheric CO2 (i.e., increasing the ocean seawater's alkalinity increases the ocean's ability to absorb/capture atmospheric CO2). Moreover, because the generated base substance is fully dissolved in the ocean alkalinity product, the electrochemical OAE approach avoids problems associated with other OAE approaches (e.g., dissolution kinetics issues that are associated with conventional mineral OAE approaches).\|[0011] Although electrochemical OAE approaches show great potential in mankind's efforts to combat global warming and ocean acidification, their widespread acceptance as a suitable NET may be predicated on the continued development of OAE system features that minimize cost per unit of captured/removed atmospheric CO2 (LCOC). For economic reasons related to carbon offsets and trading, NETs having relatively low LCOC ratings are typically favored over NETs exhibiting relatively high LCOCs. When calculating a NET's LCOC rating, many factors are taken into consideration, including capital costs (e.g., construction and installation expenses), and ongoing operating costs (e. g., land, water, maintenance, and electrical power expenses). In the case of OAE systems, the amount of atmospheric carbon removed from the atmosphere over an ocean depends on the amount of base substance supplied to the ocean (i.e., by way of the ocean alkalinity product), whereby the LCOC of an OAE system is predominantly determined by its levelized cost of producing each unit of base substance. In terms of the capital cost components of LCOC, OAE systems have an advantage over many NETs in that OAE systems are relatively inexpensive to construct and install, have a relatively small footprint and can be controlled using automated operating systems. Moreover, due to the high energy consumption and wear-related part replacement costs associated with performing the electrochemical salt-conversion process (described above), the most significant operating costs associated with an OAE system arise in the operation of the OAE system's BPED. Therefore, developments that reduce BPED operating costs arguably provide the most promising way to reduce OAE system LCOC.\|[0012] The BPEDs currently utilized in OAE systems are referred to herein as 3-chamber BPEDs for brevity. Such 3-chamber BPEDs may be characterized by utilizing an electrodialysis apparatus having an ion exchange (IE) stack configured in a 3-chamber cell arrangement, and by utilizing a flow control system capable of directing three different aqueous solutions (i.e., a salt feedstock solution, an acid solution, and a base solution) through corresponding salt/acid/base chambers of the IE stack. The IE stack includes multiple 3-chamber cells arranged in series between opposing electrodes, where each 3-chamber cell includes salt, acid and base chambers that respectively serve as parallel flow channels for the aqueous salt, acid and base solutions as they pass through the IE stack (i.e., each cell includes a salt chamber that channels a portion of the salt feedstock solution, an acid chamber that channels a portion of the aqueous acid solution, and a salt/base chamber that channels a portion of the base solution). Each cell's salt chamber is disposed between and separated from the cell's acid and salt/base chambers by corresponding ion exchange membranes, which are configured to facilitate the transfer of sodium and chloride ions from the salt chamber into the base and acid chambers during the electrochemical process. That is, during the electrochemical process an electric field applied across the IE stack by the electrodes produces an ionic current in a direction perpendicular to the parallel flow paths, whereby anions in the salt/base/acid streams (e.g., chloride ions (Cl−) and hydroxide ions (OH−)) move toward the positive electrode (anode) and cations in the salt/base/acid streams (e.g., sodium ions (Nat) and protons (H+)) move toward the positive electrode (anode). This ionic current causes dissociated salt molecules (i.e., sodium ions (Na+) and chloride ions (Cl−)) to exit the salt feedstock stream in opposite directions (i.e., such that the chloride ions (Cl−) pass through a first ion exchange filter from the cell's salt chamber into the cell's acid chamber, and the sodium ions (Nat) pass through a second ion exchange filter into the acid chamber). The chloride ions (Cl−) then combine with protons (H+) to form “new” acid (HCl) molecules in the acid solution stream passing through each cell's acid chamber, and the sodium ions (Nat) combine with hydroxide ions (OH−) to form “new” base (NaOH) molecules in the base solution stream passing through each cell's salt/base chamber. As a result of this electrochemical salt-conversion process, the base solution exiting the IE stack, which combines the base solution flows exiting each of the cells, has a significantly higher concentration of base substance (e.g., NaOH molecules) than before entering the IE stack. Similarly, the acid solution exiting each cell has a higher concentration of acid substance (e.g., HCl molecules) than before entering the IE stack. That is, the 3-chamber IE stack arrangement is configured such that three separate streams exit the ED apparatus: a reduced-salt solution stream (i.e., having a lower salt content than the salt feedstock solution fed into the ED apparatus), an acid product (strong acid) stream including the “new” acid molecules, and a base product (strong base) stream including the “new” base molecules.\|[0013] The main operational costs associated with 3-chamber BPEDs include the cost of externally supplied electricity and maintenance (e.g., replacement part and manual labor) associated with the IE stack, flow control system and other BPED subsystems required to perform the electrochemical salt-conversion process. A majority of the externally supplied electricity needed to power a given BPED operations is consumed by the IE stack (i.e., to generate the electric field that produces the ionic current) and varies in accordance with the BPED's IE stack arrangement. That is, larger capacity IE stacks (i.e., those capable of generating larger amounts of base substance per hour) typically require a larger number of series-connected cells. Although the salt/acid/base solutions are conductive, each ion exchange membranes functions like a resistor that impedes the applied electric field. Therefore, larger capacity IE stacks require larger amounts of externally supplied electricity to maintain an electric field at a suitably strong level across a larger number of cells (i.e., across a larger number of ion exchange membranes) than that required by smaller capacity IE stacks. Moreover, a significant amount is needed to power the flow control system (e.g., the various pumps and valves required to maintain the pressures and flow rates of the salt/acid/base solution streams) and other BPED subsystems, such as feedstock pretreatment units that are typically utilized to remove solids and other contaminants (e.g., divalent ions) from the aqueous salt feedstock solution (e.g., seawater) in order to reduce fouling (e.g., mineral scaling) in the IE stack. BPED maintenance costs include the cost of replacing parts that periodically wear out during normal BPED operations, costs associated with service/labor required to replace these parts, and costs associated with maintenance-related down-time (i.e., the periods of OAE system non-operation that are required to perform maintenance operations). Similar to the cost of externally supplied electricity, maintenance costs are typically higher for BPEDs with larger capacity IE stacks than BPEDs with lower capacity IE stacks due to the need to periodically replace a greater number of expensive ion exchange membranes and the higher expense associated with the replacement of flow control system and pretreatment unit components capable of the required higher flow capacities. Because the effectiveness of OAE systems as a NET is strongly dependent on minimizing LCOC (i.e., minimizing the levelized cost of producing base substance), and because the cost of externally supplied electricity and maintenance costs (e.g., the cost of ion exchange filters/membrane replacement) represent two of the most significant expenses associated with an OAE system's production of base substance, there is a strong motivation to optimize OAE system operations in a way that minimizes these two cost components.\|[0014] Enhanced ocean weathering (EOW) represents another promising ocean capture approach that both reduces atmospheric CO2 and mitigates ocean acidification. EOW involves spreading finely ground alkaline aggregate (e.g., silicate rock, such as basalt) onto large ocean surface areas. The widely dispersed alkaline aggregate captures large amounts of dissolved CO2 while in contact with the ocean water. The alkaline aggregate then sinks below the surface, thereby storing the captured CO2 in the ocean and slowing ocean acidification by way of direct interaction between the ocean's seawater and the alkaline material. A major challenge faced by EOW technologies is how to maximize CO2 drawdown for a given amount of finely ground alkaline aggregate. Currently, the best strategies for addressing this challenge at scale involve crushing/grinding the alkaline rock into extremely small particles and then dispersing these particles over large areas of the ocean to maximize the ratio of surface area to dispersed volume. A problem with these EOW strategies is that both the crushing/grinding and dispersing processes require a significant amount of energy. As explained above, the effectiveness of EOW systems as a NET is strongly dependent on minimizing LCOC, and because the cost of externally supplied electricity to crush/grind the alkaline rock represents one of the most significant expenses associated with an EOW system, there is a strong motivation to optimize EOW system operations in a way that minimizes this cost component.\|[0015] Seawater desalination is the process of removing salt and other contaminants from seawater, making it suitable for human consumption, irrigation, or industrial uses. Seawater desalination allows coastal communities to use a broader variety of water sources than conventional techniques, improving the resilience of water-stressed communities. Seawater desalination will become increasingly important as climate change threatens traditional water resources. As sea levels rise, existing freshwater aquifers for coastal communities are at an increasingly high risk of seawater intrusion, thereby making seawater desalination an important potential tool to help these communities adjust to climate change.\|[0016] Seawater desalination systems utilize either thermal technologies or membrane-based technologies. Thermal desalination systems heat seawater so that H2O evaporates into steam, leaving behind salt and other impurities, then condenses the steam back into liquid freshwater that is suitable for human consumption or other freshwater uses. Membrane-based desalination describes a class of technologies in which saline water passes through a semi-permeable material that allows H2O through but holds back dissolved solids like salts. Reverse osmosis is the most common membrane-based desalination technology that reverses the natural osmosis process (i.e., the natural movement of freshwater from an area of low salt concentration to an area of high salt concentration) by utilizing high-energy pumps to pressurize seawater located on a first side of a semi-permeable material such that passes through the membrane to generate freshwater (sometimes referred to as permeate) on the opposing (second) side of the membrane and leaving behind high-salt content brine (i.e., aqueous solution having a significantly higher salt content than that of seawater) on the first side of the membrane. Note that the pressure required to force freshwater through a membrane is directly proportional to the feedstock solution's salt content (i.e., saltier water having a relatively high salt concentration requires more pressure than less salty water), but this pressure is limited by the strength of the membrane (i.e., the membrane will rupture if the pressure is too high). Therefore, the strength of the membrane effectively creates an upper limit on the salinity of water that can be treated at a given flow volume, and a feedstock solution having a salt content much higher than seawater typically cannot be purified using reverse osmosis technologies.\|[0017] Problems associated with all seawater desalination technologies are related to the disposition of brine, high operating costs and carbon footprint. Both thermal and membrane-based desalination technologies generate brine having a higher salt concentration than seawater that is typically disposed of by supplying the brine into the ocean in a manner that both avoids ecological hazards (e.g., harm to sea life) and does not increase the salt content of the seawater feedstock drawn into the desalination plant (i.e., significant resources are required to disperse the brine over a large ocean region and far from the seawater feedstock input pipe). In addition, although the most efficient thermal desalination processes typically use more energy than membrane-based approaches, even reverse-osmosis seawater desalination consume large amounts of electrical energy (e.g., to drive seawater feed pumps and to achieve the pressures necessary to force permeate through semi-permeable membranes). This high energy consumption causes conventional seawater desalination plants to have both high operating costs and a large carbon footprint (i.e., due to the significant greenhouse gas emissions associated with the generation of the required electrical energy).\|[0018] What is needed is a system/method that reduces seawater desalination system operating costs (i.e., external electricity and/or maintenance) and greenhouse gas emissions while avoiding the ecological hazards and other problems associated with brine disposition. What is also needed is a carbon dioxide removal (CDR) system/method that minimizes LCOC by way of significantly reducing the operating costs associated with conventional EOAE systems/methods (i.e., external electricity and/or maintenance costs) and/or EOW systems/methods (i.e., crushing/grinding costs).\|SUMMARY OF INVENTION\|[0019] In an embodiment the present invention is directed to a modified desalination process and associated method that utilizes an electrochemical process to both mitigate the above-mentioned brine disposition problem and address other problems associated with conventional desalination systems/methods. Similar to conventional desalination processes, the modified desalination system/method is configured to convert a saltwater feedstock (e.g., brackish groundwater or seawater having an initial/first salt concentration) into a desired stream of freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a byproduct stream containing brine (i.e., saline solution having a relatively high (second) salt concentration that is higher than the initial salt content of the saltwater feedstock). According to an aspect, the modified electrochemical process is utilized to mitigate the above-mentioned brine disposition problem by effectively removing most of the salt from the brine stream in a way that effectively converts the brine stream into a reduced-salt stream having a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. According to another aspect, at least some of the reduced-salt stream generated by the electrochemical process is mixed/combined with the saltwater feedstock (i.e., such that the saltwater feedstock is effectively diluted by the reduced-salt stream before performing the desalination process), thereby reducing freshwater production costs by reducing the amount of salt that must be filtered/removed from the saltwater feedstock during the desalination process (i.e., in comparison to conventional processes in which only saltwater feedstock is desalinated).\|[0020] In an embodiment a modified desalination (or other) system includes an electrochemical reactor (e.g., a bipolar electrodialysis apparatus (BPED)), a mixing device and a desalination unit that are cooperatively coupled and configured to perform the modified desalination process mentioned above. The desalination unit utilizes known techniques to convert a saltwater feedstock having an initial (first) salt concentration into a freshwater stream and a brine stream having a relatively high (second) salt concentration, and the system is configured to direct (e.g., by way of pipes and pumps) the brine stream from an output terminal of the desalination unit to an input terminal of the electrochemical reactor. The electrochemical reactor is configured to channel three separate solutions: an aqueous salt solution that enters the reactor as the brine stream and exits as the reduced-salt stream, an aqueous acid solution that enters as a weak acid stream and exits as an acid product stream, and an aqueous base solution that enters as a weak base stream and exits as a base product stream. The electrochemical reactor is also configured to generate the reduced-salt stream by electrochemically processing the brine stream such that at least some of the salt molecules (e.g., NaCl) contained in the brine stream are converted into acid molecules (HCl) contained in the acid product stream and base molecules (NaOH) contained in a base product stream. According to another aspect, the electrochemical processing is performed at a rate that converts/removes a sufficient amount salt from the salt/saline solution such that the (third) salt concentration of the reduced-salt stream leaving the electrochemical reactor is lower than the initial (first) salt concentration of saltwater feedstock, thereby significantly reducing eco-safety risks and other brine disposition issues associated with conventional desalination systems/processes. According to another aspect, the system is further configured to direct (e.g., by way of pipes and pumps) at least some of the reduced-salt stream from the electrochemical reactor to an input terminal of the mixing device, which is configured to mix a saltwater feedstock stream (i.e., untreated feedstock or treated feedstock) with the reduced-salt stream received from the electrochemical reactor such that the resulting mixture stream has a (fourth) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock, and the desalination unit is configured to generate the freshwater stream and the brine stream by processing the mixture stream (desalination fluid) exiting the mixing device. Mixing (combining) the saltwater feedstock with the reduced-salt stream provides the system with two cost-saving benefits over conventional desalination systems: first, the energy cost required to produce each unit of freshwater is reduced because the amount of raw seawater or briny groundwater that must be pumped from a saltwater feedstock source to the desalination unit is reduced by an amount equal to that of the reduced-salt stream; and second, the operating/maintenance costs of the system are reduced by reducing the amount of salt that must be filtered or otherwise separated from the desalinated fluid (i.e., the feedstock/reduced-salt mixture) by the desalination unit. Accordingly, by utilizing an electrochemical reactor to remove salt from the brine stream generated by the desalination process, and then utilizing the reduced-salt stream generated by the electrochemical reactor to supplement/dilute the saltwater feedstock directed into the desalination unit, the modified desalination system both mitigates the above-mentioned brine disposition problem and addresses other problems associated with conventional desalination systems.\|[0021] In some embodiments, the system includes an optional pretreatment unit that is operably coupled between a saltwater feedstock source (e.g., ocean or well) and the mixing device, and is configured to remove solids and other contaminants from a stream (portion) of “raw” saltwater feedstock that has been pumped or otherwise delivered from the saltwater feedstock source (e.g., seawater pumped directly from an ocean or briny groundwater pumped from a well), and is further configured to deliver the resulting treated saltwater feedstock to the mixing device by way of the saltwater feedstock stream. In some embodiments the pretreatment unit includes filtering systems or other devices that function to remove solids and at least some contaminants (e.g., biological material and/or divalent ions) from the received raw saltwater feedstock. In an exemplary embodiment, the pretreatment unit includes one or more series connected filtering devices that utilize associated filters to remove contaminants from raw saltwater feedstock (e.g., a first filtering system that utilizes first filter(s) to remove solid particles from seawater, and a second filtering system that utilizes second filter(s) to selectively remove metals and/or biologic materials of value from the partially filtered seawater/brine received from the first filtering system). The filtered contaminants (e.g. removed solids, metals and/or biological materials) are removed from the feedstock flow path using known techniques, and the resulting treated (filtered) feedstock solution (i.e., the treated saltwater feedstock solution that has passed through the filters) forms the saltwater feedstock stream that is passed downstream to the mixing device for mixing with the reduced-salt stream received from the electrochemical reactor). In another exemplary embodiment, the pretreatment unit includes nanofiltration, ultrafiltration, chemical precipitation or other water purification system(s) that is/are configured to remove contaminants and reduce the hardness of the saltwater feedstock by filtering/removing dissolved metal ions and other hardness related minerals (e.g., calcium (Ca2+), magnesium (Mg2+), carbonate (CO3)2−, and iron (Fe2+/Fe3+)), and the system may be configured to return the filtered/removed hardness related minerals to the ocean by way of the ocean alkalinity product. Utilizing the pretreatment unit further reduces operating and maintenance costs by extending the uninterrupted operating period of the desalination unit. Moreover, because the reduced-salt stream is utilized as described above to reduce the required amount of raw saltwater feedstock, the cost of maintaining pretreatment units is lower than that of conventional desalination systems (i.e., reducing the amount of saltwater feedstock passed through the pretreatment unit reduces the rate of filter replacement or other periodic maintenance). In some embodiments a second ion removal process (e.g., filtering similar to that used to remove harness related minerals) is applied to the byproduct brine stream leaving the desalination unit (i.e., before the brine stream is supplied to the electrochemical reactor 110E), thereby further reducing operating costs. In other embodiments, the pretreatment unit may be omitted, for example, in cases where the raw saltwater feedstock is sufficiently free of contaminants when delivered to the desalination system.\|[0022] In some embodiments, the mixing device is configured to generate the mixture stream supplied to the desalination unit at a constant outflow rate by combining all of the reduced-salt stream received from the electrochemical reactor with a corresponding portion of the treated/untreated saltwater feedstock. As mentioned above, the salt content of the mixture stream exiting the mixing device is inversely proportional to the respective inflow rates of the reduced-salt stream and the saltwater feedstock, so minimizing the mixture stream's salt content (and thus minimizing desalination operating/maintenance costs) involves admitting as much of the reduced-salt stream as possible into the mixing device. In cases where the outflow rate of the mixture stream is determined by the combined reduced-salt stream and saltwater feedstock inflow rates, and is maintained constant (e.g., at the maximum processing rate of the desalination unit), the constant mixture stream outflow rate is achieved by admitting the total amount/inflow of the reduced-salt stream delivered to the mixing device and the controlling (i.e., increasing or decreasing) the saltwater feedstock inflow rate such that the combined inflow rates equal the constant mixture stream outflow rate. In some embodiments, a sensor monitors the flow rate of the reduced-salt stream delivered to the mixing device and a feedstock flow control device is utilized to control a (first) inflow rate of the saltwater feedstock stream into the mixing device, where the system controller controls the feedstock flow control device such that the (first) inflow rate is adjusted (increased/decreased) in accordance with changes (decreases/increases) in the (second) inflow rate of the reduced-salt stream into the mixing device. In some embodiments, the mixing device includes a mixing tank that receives the reduced-salt stream exiting the ED apparatus and a treated saltwater feedstock stream exiting a pretreatment unit such that the two streams intermix within the tank to form the mixture stream. In other embodiments, the mixing device may be implemented, for example, using interconnecting pipes or other mixing structures.\|[0023] As set forth above, the desalination unit functions to desalinate the mixture stream received from the mixing device to generate freshwater and the high-salt brine/feedstock stream. In some embodiments, the desalination unit utilizes a known desalination device/process (e.g., thermal desalination or membrane-based desalination) to separate the mixture stream into the desired freshwater (permeate) stream and the byproduct brine stream. In an exemplary embodiment, the desalination unit utilizes a reverse osmosis (RO) system including a semi-permeable membrane that prevents the passage of salt molecules, whereby the brine stream is formed on one side of the membrane and permeate (freshwater) passes to the opposing side of the membrane. Similar to conventional desalination processes, the freshwater generated by the desalination unit has a suitably low salt concentration (e. g., ≤500 ppm), and the brine stream comprises an aqueous solution having salt content greater than 50,000 ppm (5%).\|[0024] In an embodiment the electrochemical reactor is implemented using a bipolar electrodialysis system (BPED) of a type similar to that utilized in existing OAE systems to convert the high-salt brine stream into the reduced-salt stream. The BPED includes an electrodialysis (ED) apparatus that utilizes an ion exchange stack to perform an electrochemical salt-conversion process during which salt supplied in the brine stream is converted into a base substance and an acid substance. In some embodiments, the ion exchange stack comprising a series of salt chambers, acid chambers and base chambers that are arranged in series between opposing electrodes, where each salt chamber is located between and separated from associated pair of adjacent acid and base chambers by an associated intervening ion exchange membrane. The BPED also includes a flow control system including a first portion that is configured to direct the brine stream through the salt chambers of the ion exchange stack, a second portion configured to direct an aqueous acid solution through the acid chambers and a third portion configured to direct an aqueous base solution through the base chambers. During operation the opposing electrodes apply an electric field across the ion exchange stack to electrochemically process salt (e.g., NaCl) in the brine stream disposed in each salt chamber such that chlorine ions (Cl−) pass through first ion exchange membranes and combine with dissociated protons (H+) to form “new” acid molecules (HCl) in the aqueous acid solution disposed in the associated adjacent acid chamber, and such that sodium ions (Na+) pass through second ion exchange membranes and combine with dissociated hydroxide ions (OH−) to form “new” base molecules (NaOH) in the aqueous base solution disposed in the associated adjacent base chamber. In this manner, the electrochemical process causes the acid and base product streams leaving the ED apparatus to have a higher acid and base concentrations, respectively, than the acid/base solutions entering the ED apparatus. Conversely, the electrochemical process causes the reduction (removal) of salt from the brine solution passed through the ED apparatus, whereby the reduced-salt solution stream exiting the ED apparatus has a salt concentration that is substantially lower than that of the brine stream entering the ED apparatus. By utilizing a BPED similar to those used in stand-alone OAE systems (or another electrochemical reactor having a similar salt processing capacity), the reduced-salt solution can be generated with a salt concentration that is equal to or lower than that of seawater (e.g., below 35,000 ppm (3.5%)), thereby addressing the brine disposition issues associated with stand-alone desalination plants.\|[0025] In some embodiments, the electrochemical reactor also includes a fluid buffering system including an acid buffer tank and a base buffer tank that facilitate the circulation of the aqueous acid and base solutions through the ED apparatus. Specifically, the acid buffer tank is configured to contain the aqueous acid solution that is directed (by way of associated flow control elements) into the acid (second) chamber(s) of the ion exchange stack and to receive a first portion of the acid product stream exiting (directed away from) the acid chambers(s). Similarly, the base buffer tank is configured to contain the aqueous base solution that is directed to the base (third) chamber(s) of the ion exchange stack and to receive a first portion of the base product stream exiting the base chamber(s). Note that second portions of the acid and base product streams are typically diverted for other purposes (e. g., maintenance, OAE or commercial sale). As mentioned above, the electrochemical reactor's flow control system is configured such that the brine stream exiting the desalination unit is directed to the ED apparatus, and at least a portion of the reduced-salt stream exiting the ED apparatus is directed to the mixing device. This salt solution flow arrangement differs from BPEDs utilized in conventional OAE systems in which the reduced/depleted salt stream exiting an ED apparatus is typically utilized to replenish (make up) any acid/base product diverted from the electrochemical reactor for other purposes and to control the acid/base concentration (dilution) of the weak acid and base solutions directed to the ED apparatus. To facilitate dilution of the acid and/or solution streams in cases where all of the reduced-salt stream is directed to the mixing device, in one embodiment, the flow control system is further configured to divert some of the freshwater stream exiting the desalination unit such that it flows into the acid buffer tank and/or the base buffer tank. Although utilizing some of the freshwater for acid and/or base dilution reduces the amount of freshwater output from the system, the required dilution amount is typically much less than that produced by the desalination unit, and may provide a net benefit, for example, in cases where high quality acid product is desired (i.e., the acid product's value is typically inversely proportional to the amount of salt in the acid solution). In other embodiments, replenishing for the acid and/or base product streams may be achieved using a portion of the reduced-salt stream or using a mixture of both freshwater and reduced-salt streams.\|[0026] In some embodiments the brine stream exiting the desalination unit may be passed directly to the ED apparatus (i.e., the fluid buffer system may only include an acid buffer tank and a base buffer tank, and omit a salt buffer tank). In other embodiments, the fluid buffer system may include a salt buffer tank that is operably coupled between the desalination unit and the ED apparatus, and serves as a buffer for aqueous salt solution (i.e., such that a portion of the brine stream produced by the desalination unit is stored in the salt buffer tank). In this case, the salt buffer tank may be used to regulate the flow rate of brine into the ED apparatus.\|[0027] In some embodiments, the electrochemical reactor is configured to process brine at a rate that corresponds with a desired maximum freshwater production rate. That is, a desalination unit that is capable of generating freshwater at a relatively high flow rate also generates brine at a relatively high flow rate, so, to avoid the buildup of unprocessed brine, the electrochemical reactor must be capable of converting the brine stream into a corresponding reduced-salt stream at a corresponding flow rate. In addition to suitable flow control and buffer resources, the electrochemical reactor's ED apparatus must be configured to receive and process brine at the corresponding flow rate, for example, by way of providing a sufficient number of cells (i.e., groups of salt, acid and base chambers separated by intervening ion exchange membranes) arranged in series between suitable electrodes, and otherwise configuring the ED apparatus to facilitate the conversion of brine at the relatively high flow rate.\|[0028] In another exemplary embodiment, an integrated (combined) desalination/OAE system includes a seawater desalination subsystem and an OAE subsystem (electrochemical reactor). The seawater desalination subsystem generates a freshwater stream by desalinating seawater pumped or otherwise drawn from a nearby ocean using any of the desalination processes mentioned above. The OAE subsystem includes an ED apparatus that converts salt provided in the byproduct brine stream from the desalination process into acid and base product streams. The system also includes a post-production unit that selectively utilizes a portion of the base product stream to generate an ocean alkalinity product and selectively utilizes a portion of the acid product stream to generate an alkaline slurry, and then supplies (e.g., pumps) the ocean alkalinity product and the alkaline slurry to the ocean at a designated outfall location for OAE and enhanced ocean weathering (EOW) purposes (i.e., such that both the fully dissolved base substance in the ocean alkalinity product and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification). Integrating seawater desalination and at least one of OAE or EOW operations in the manner set forth herein essentially eliminates the ecological concerns associated with conventional stand-alone seawater desalination and significantly decreases total operating costs (i.e., in comparison with conventional stand-alone seawater desalination). That is, because the brine stream has a higher salt concentration than seawater, electrochemically processing the brine stream (i.e., in place of seawater) enhances the generation of ocean alkalinity product by decreasing the amount of externally supplied energy that is required to perform the electrochemical conversion of salt molecules (e.g., NaCl) into acid molecules (e.g., HCl) and base molecules (e.g., NaOH) for a given flow rate through the electrochemical reactor, thereby increasing the base product production efficiency and decreasing total operating cost over conventional stand-alone OAE systems that process seawater, thereby reducing LCOC in comparison to such OAE systems. Moreover, by generating and supplying alkaline ocean product and alkaline slurry to the ocean, the resulting OAE effectively offsets the carbon footprint of the seawater desalination process, and the integrated desalination/OAE system achieves greatly reduces total operating costs over separate (stand-alone) desalination and OAE plants. In addition, utilizing the reduced-salt stream, which is generated as a byproduct of the OAE process, to supplement the seawater (saltwater feedstock) processed by the desalination subsystem reduces operation and maintenance costs over conventional stand-alone seawater desalination plants, for example, by reducing the amount of raw seawater that must be pumped from an ocean and pretreated before desalination. Further, utilizing an electrochemical reactor to process the brine stream that is generated as a byproduct of the desalination process provides additional advantages including: (1) reducing environmental issues and dispersion costs associated with releasing high-salt-content brine directly from the desalination process into an ocean; and (2) reduces maintenance costs by facilitating the use of the generated acid product (e.g., HCl), e.g., to clean semi-permeable and/or ion exchange membranes utilized in the ion exchange stack. Moreover, integrating seawater desalination and OAE subsystems facilitates other benefits such as capital expense reductions achieved by shared plant facilities (e.g., project site and shelter/building), shared saltwater feedstock intake/outfall structures and associated operating costs, shared water treatment operating costs, and shared electrical infrastructure. Further, permitting (government authorization) for desalination plants is difficult in some regions because of eco-safety risks that are primarily due to the increased salinity of the outfall brine—the present invention mitigates this eco-safety risk by utilizing an electrochemical reactor to process the brine such that its final salinity is closer to ambient conditions, thereby leading to an easier permitting process for desalination plants modified in the manner described herein.\|[0029] Although described herein with specific reference to specific modified desalination and integrated desalination/OAE/EOW systems/methods, the present invention may also be utilized to provide other commercially advantageous operations that may achieve at least some of the benefits set forth above. For example, the base product and/or acid product generated by the electrochemical reactor/process may be selectively utilized for non-OAE uses. Although the carbon footprint of the resulting desalination system/process may be higher than that of the combined desalination/OAE approach, the desalination system/process would still have advantages over conventional seawater desalination operations. That is, utilizing the electrochemical reactor to reduce the salt content of the high-salt brine/feedstock stream significantly reduces eco-safety risks and other issues associated with the disposition of the high-salt brine generated by conventional desalination processes. In an exemplary embodiment, the system's controller may monitor one or more sites that provide input data including spot pricing for the base product and/or acid product generated by the electrochemical reactor. The controller may then utilize this input data to determine whether the base and/or acid products should be utilized for OAE/EOW purposes, or whether they should be sold to a third-party buyer. For example, when sufficient low/zero-carbon electricity is available from a power grid to offset the desalination process carbon footprint and the base product spot price is sufficiently high, then the controller may direct the post-production unit to divert the base product (e.g., some or all of the second base stream portion) for sale to a third-party buyer (i.e., instead of directing the base product to the ocean as part of ocean alkalinity product), whereby proceeds from the sale serve to reduce total operating costs of the system. Similarly, the control algorithm implemented by the system's controller may monitor input data from one or more sites that provide spot pricing for the acid product (e.g., HCl) generated by the electrochemical reactor, and utilizes this data to determine whether it is more cost effective to neutralize the acid product (e.g., by way of enhanced ocean weathering), or if selling the acid product may produce a greater value (i.e., if the acid product spot price is sufficiently high), in which case the controller may direct the post-production unit to divert the acid product (e.g., some or all of the second acid stream portion) for sale to a third-party buyer.\|[0030] According to another embodiment, a hybrid carbon dioxide removal (CDR) system includes an electrochemical OAE subsystem configured to generate an ocean alkalinity product, an EOW subsystem configured to generate an alkaline slurry, and a base delivery subsystem configured to supply at least one of the ocean alkalinity product and the alkaline slurry to an ocean to capture/reduce atmospheric carbon dioxide and mitigate ocean acidification. The electrochemical OAE subsystem utilizes an ED device configured to electrochemically process/convert salt into an acid substance and base substance and utilizes an alkaline product generator to generate an ocean alkalinity product including the base substance. In an exemplary embodiment, the EOW subsystem includes an accelerated ocean weathering reaction apparatus and a slurry generator. The accelerated ocean weathering reaction apparatus is configured to combine the acid substance from the electrodialysis device with an alkaline aggregate such that an accelerated ocean weathering reaction between the alkaline aggregate and the acid substance both neutralizes the acid substance and etches/weakens the alkaline aggregate. The slurry generator then receives the neutralized (fully processed) process fluid exiting the reaction apparatus and processes the etched/weakened alkaline aggregate into fine particles, thereby forming the alkaline slurry. In some embodiments, metal elements are released from the alkaline aggregate during the accelerated weathering and slurry generation processes and are reclaimed from the alkaline slurry to offset operating costs. The base delivery subsystem is configured to supply at least one of the ocean alkalinity product and the alkaline slurry to the ocean. By utilizing the acid substance of the electrochemical process to etch/weaken the alkaline aggregate, the accelerated (electrochemically assisted) ocean weathering process implemented by the EOW subsystem produces alkaline slurry at a significantly reduced cost in comparison to conventional EOW systems. That is, the acid substance, which is a byproduct of the electrochemical process and is therefore essentially cost free, serves to etch/weaken the alkaline aggregate, thereby increasing the etched/weakened aggregate's specific surface area and/or facilitating crushing/grinding the etched/weakened aggregate into alkaline particles suitable for ocean dispersal offsetting energy than would be required by conventional EOW crushing/grinding operations. Moreover, during the accelerated weathering operation the alkaline material in the alkaline aggregate neutralizes the acid substance, thereby circumventing acid storage/neutralization issues associated with conventional OAE technologies. Further, by supplying both the electrochemically generated ocean alkalinity product and the alkaline slurry to the ocean, the hybrid CDR system achieves at least the same amount of carbon capture removal and ocean deacidification as that achieved by independently operated conventional OAE and EOW systems using significantly less energy than separate conventional OAE and EOW systems. In some embodiments the CDR system utilizes a desalination subsystem to convert seawater from the ocean into a high-salt-content brine in order to enhance the electrochemical process.\|(US20250339810)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0031] FIG. 1 shows a modified desalination system according to an exemplary embodiment of the present invention;\|[0032] FIG. 2 shows a simplified electrochemical reactor that may be utilized to electrochemically process a brine solution in the modified desalination system of FIG. 1, according to an exemplary specific embodiment;\|[0033] FIG. 3 shows a simplified electrodialysis apparatus that may be utilized by the electrochemical reactor of FIG. 2 to electrochemically convert salt into acid and base products according to another exemplary embodiment;\|[0034] FIG. 4 shows a modified desalination system according to another exemplary embodiment; and\|[0035] FIG. 5 shows an integrated desalination/OAE/EOW system according to another exemplary embodiment of the present invention; and\|[0036] FIG. 6 shows an EOW subsystem of the integrated desalination/OAE/EOW system of FIG. 5 in additional detail according to an exemplary embodiment.\|(US20250339810)\|DETAILED DESCRIPTION\|[0037] The present invention combines desalination and electrochemical systems/processes in a way that converts a saltwater feedstock (e.g., seawater or briny groundwater) into freshwater suitable for human consumption and other freshwater uses, a base substance suitable for OAE purposes, and an acid substance. The invention is primarily described herein with specific reference to a modified desalination system/method that utilizes a desalination subsystem/process to convert saltwater feedstock into freshwater and brine and utilizes an electrochemical reactor/process to convert the brine into a reduced salt solution (i.e., by converting salt in the brine into acid and base substances). In one embodiment, the invention is described with reference to an integrated desalination/OAE/EOW system/method that desalinates seawater to produces freshwater and brine, electrochemically processes the brine to generate acid and base products, utilizes the base product to perform an OAE process, and utilizes the acid product to reduce the energy costs associated with crushing/grinding alkaline aggregate in an EOW process. However, in some embodiments, the systems/methods described herein may be utilized for other purposes, including a stand-alone hybrid HDR system/method or a system/method for generating acid and/or base substances in remote locations. The following description is presented to enable one of ordinary skill in the art to make and use the methods and systems described herein as provided in the context of specific embodiments. Various modifications to the embodiments will be apparent to those with skill in the art, and the general principles defined herein may be applied to other embodiments. Therefore, the methods and systems described herein are not intended to be limited to the particular embodiments shown and described, but are to be accorded the widest scope consistent with the principles and novel features herein disclosed.\|[0038] FIG. 1 depicts a modified desalination system 100 including an electrochemical reactor 110, a desalination subsystem 160 and a system controller 190. Electrochemical reactor 110 performs an electrochemical process in which a high-salt-content brine stream 111-1 is received from the desalination subsystem 160, salt contained in brine stream 111-1 is electrochemically processed (removed), and then at least a portion 111-21 of the resulting reduced-salt stream 111-2 is directed back to desalination subsystem 160. Desalination subsystem 160 performs a modified desalination process in which a mixing device 170 mixes (combines) a saltwater feedstock stream 51T (e.g., seawater or briny groundwater) with reduced-salt stream portion 111-21 received from electrochemical reactor 110 to form a mixture stream 51M, and then a desalination unit 180 processes (desalinates) mixture stream 51M to generate a freshwater stream 115 (i.e., water suitable for human consumption, irrigation, or industrial uses) and brine stream 111-1, which is directed to electrochemical reactor 110. System controller 190 controls the various operations performed by electrochemical reactor 110 and desalination subsystem 160 such that at least a portion of freshwater 115 exiting desalination subsystem 160 is directed out of system 100 as freshwater output stream 115-OUT for fresh water uses. Additional details regarding the various components and processes of system 100 are set forth below.\|[0039] Referring to the left side of FIG. 1, desalination subsystem 160 includes an optional pretreatment unit 165, a mixing device 170 and a desalination unit 180 that process saltwater feedstock 51 to generate freshwater stream 115 and brine stream 111-1.\|[0040] Optional pretreatment unit 165 is configured to treat a “raw” saltwater feedstock stream 51 (i.e., feedstock received directly from an external source, such as raw seawater pumped from an ocean 50, or briny groundwater pumped from a well) by removing (e.g., filtering) solids and other contaminants (e.g., biological material and/or divalent ions) from the raw feedstock. The resulting treated saltwater feedstock exiting pretreatment unit 165 is then supplied to mixing device 170 as saltwater feedstock stream 51T. Note that optional pretreatment unit 165 does not significantly reduce or otherwise change the salt content of the saltwater feedstock (i.e., the treated saltwater forming saltwater feedstock stream 51T has substantially the same initial (first) salt concentration as the raw saltwater forming feedstock stream 51. Pretreatment unit 165 may be omitted, for example, is cases where raw saltwater feedstock stream 51 is sufficiently pure (i.e., free of contaminants), or in embodiments where the raw saltwater feedstock is treated prior to being delivered into desalination subsystem 160. When pretreatment unit 165 is omitted, raw saltwater feedstock is passed directly to mixing device 170 (i.e., saltwater feedstock stream 51T and raw saltwater feedstock stream 51 comprise the same saltwater feedstock stream).\|[0041] Mixing device 170 is configured to receive reduced-salt stream portion 111-21 from electrochemical reactor 110 (i.e., some or all of reduced-salt stream 111-2 exiting ED apparatus 130) and saltwater feedstock stream 51T from pretreatment unit 165. Mixing device 170 utilizes one or more mechanisms (e.g., a mixing tank and/or pumps) to mix (combine) the two streams and to produce a mixture stream 51M including a mixture solution having a (fourth) salt concentration that is between the initial (first) salt concentration of saltwater feedstock stream 51T and an intermediate (third) salt concentration of the reduced-salt stream 111-21. As described in additional detail below, electrochemical reactor 110 is configured to generate reduced-salt stream 111-2 such that the intermediate (third) salt concentration is lower than the initial (first) salt concentration of saltwater feedstock stream 51T. Therefore, mixture stream 51M comprises an aqueous solution having a salt concentration that is lower than the initial salt concentration of the saltwater feedstock. An outlet of mixing device 170 is operably coupled to an inlet of desalination unit 180 such that mixture stream 51M is directed into desalination unit 180. In some embodiments (not shown), the mixing process performed by mixing device 170 may be implemented by either optional pretreatment unit 165 or desalination unit 180.\|[0042] In some embodiments mixing device 170 is configured to generate mixture stream 51M by combining all of reduced-salt stream 111-21 received from electrochemical reactor 110 with a corresponding portion of the treated/untreated saltwater feedstock included in saltwater feedstock stream 51T. That is, the flow rate of mixture stream 51M exiting mixing device 170 is substantially equal to a sum of the inflow rate of reduced-salt stream 111-21 received from electrochemical reactor 110 and the inflow rate of saltwater feedstock stream 51T. In this preferred embodiment, mixture stream 51M includes the total amount of reduced-salt stream 111-21 received from electrochemical reactor 110 and adjusts, if necessary, the inflow rate of saltwater feedstock stream 51T (e.g., by way of a feedstock flow control device 171). For example, assuming desalination unit 180 is configured to process mixture stream 51M at a total flow rate of 100 units per minute, if electrochemical reactor 110 provides reduced-salt stream 111-21 to mixing device 170 at an inflow rate of 30 units/min then the corresponding inflow rate of saltwater feedstock stream 51T is adjusted to equal 70 units/min, and if electrochemical reactor 110 subsequently provides reduced-salt stream 111-21 at an inflow rate of 35 units/min then the corresponding inflow rate of saltwater feedstock stream 51T is adjusted to 65 units/min. Utilizing all of the available reduced-salt stream 111-21 to generate mixture stream 51M minimizes the amount of salt that must be removed from mixture stream 51M by desalination unit 180 (i.e., by minimizing the proportion of saltwater feedstock to reduced-salt solution in mixture stream 51M). Note that variations in the inflow rate of reduced-salt stream 111-21 may occur for purposes of project wide optimization. For example, when acid production is valued higher than freshwater and base production, then freshwater stream portion 115-2 may be directed to acid buffer tank 121-2 (i.e., to increase the value of acid product stream 112-2 by minimizing salt content), whereby more of reduced-salt stream 111-2 may be directed to mixing device 170 as reduced-salt stream portion 111-21. In other cases it may be determined that freshwater and/or base production may be optimized when both freshwater stream portion 115-2 and reduced-salt stream 111-22 are simultaneously directed to acid buffer tank 121-2 and/or base buffer tank 121-3, where the system controller adjusts the fractions of the freshwater and reduced-salt streams to optimize the salt content in the acid and base solutions. In other embodiments, system optimization may be achieved by replenishing (making-up) for the acid product stream 112-22 and/or base product stream 113-22 using only reduced-salt stream portion 111-22 with the remainder of reduced-salt stream 111-2 being directed to mixing device 170 as reduced-salt stream portion 111-21. Whenever system optimization requires a corresponding change (increase/decrease) in the inflow rate of salt stream portion 111-21 to mixing device 170, the system controller makes a corresponding adjustment (decrease/increase) to the inflow rate of saltwater feedstock stream 51T so that the outflow rate of mixture stream 51M remains constant.\|[0043] Desalination unit 180 is configured to perform a desalination process on mixture stream 51M in a manner that generates high-salt brine stream 111-1, which is then directed to electrochemical reactor 130, and freshwater stream 115 comprising water having a salt concentration that is suitable for human consumption (e.g., less than or equal to 0.05% (≤500 ppm). By way of example, when the saltwater feedstock comprises seawater pumped from an ocean, saltwater feedstock stream 51/51T has a salt concentration of about 3.5%, the relatively high salt concentration of brine stream 111-1 may be greater than 5%. As described in additional detail below, in alternative embodiments desalination unit 180 may be implemented using a thermal desalination system, a reverse osmosis system or another membrane-based (or other) desalination system.\|[0044] Referring to the right side of FIG. 1, electrochemical reactor 110 includes a fluid buffering system 120, an electrochemical reactor 130 and a flow control system. As set forth in additional detail below, electrochemical reactor 110 is configured to generate reduced-salt stream 111-2 by electrochemically processing the brine stream 111-1 such that at least some of the salt molecules (e.g., NaCl) contained in brine stream 111-1 are converted into acid molecules (e.g., HCl) contained in an acid product stream 112-2 and base molecules (NaOH) contained in a base product stream 113-2, and such that the reduced-salt stream 111-2 exiting the electrochemical reactor 110 has a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. Note that electrochemical reactor 110 is greatly simplified for descriptive purposes, and that additional details regarding its construction and operation are provided below with reference to the exemplary embodiments depicted in FIGS. 2 to 5.\|[0045] Fluid buffering system 120 includes an acid buffer tank (ABT) 121-2 and a base buffer tank 121-3. Acid buffer tank 121-2 is configured to contain an aqueous acid solution that is circulated through reactor 130 by way of associated flow control structures (e.g., pipes and pumps) such that a relatively weak acid stream 112-1 is directed from acid buffer tank 121-2 to reactor 130 and at least a portion 112-21 of a relatively strong acid product stream 112-2 leaving reactor 130 is directed back to acid buffer tank 121-2. Base buffer tank 121-3 is configured to contain an aqueous base solution that is circulated through reactor 130 by way of associated flow control structures such that a relatively weak base stream 113-1 is directed from base buffer tank 121-3 to reactor 130 and at least a portion 113-21 of a relatively strong base product stream 113-2 leaving reactor 130 is directed back to base buffer tank 121-3. In some embodiments, the flow control system is further configured to direct a portion 115-2 of freshwater 115 into one or more of acid buffer tank 121-2 and base buffer tank 121-3 to dilute the weak solutions directed into reactor 130.\|[0046] ED apparatus 130 generally includes an ion exchange (IE) stack 135 that is disposed between two electrodes (i.e., anode 138+ and cathode 138−). IE stack 135 typically includes multiple cells arranged in series between electrodes 138+ and 138−, where each cell includes three chambers that respectively serve as parallel flow channels for the aqueous salt, acid and base solutions as they pass through IE stack 135. For brevity and clarity, only one cell of IE 135 is depicted in FIG. 1, which is made up of a salt chamber 131 that functions to channel a portion of the aqueous salt solution, an acid chamber 132 that channels a portion of the aqueous acid solution, and a base chamber 133 that channels a portion of the aqueous base solution. Each cell's salt chamber 131 is disposed between and separated from the cell's acid chamber 132 and base chamber 133 by corresponding ion exchange membranes 134-1 and 134-2, which are configured to facilitate the transfer of sodium and chloride ions from the salt chamber into the base and acid chambers during the electrochemical process as described below. ED apparatus 130 also includes manifold or other structures (not shown) that are configured to cooperate with the flow control resources of BPED 110 to direct the three different (i.e., a salt, acid and base) aqueous solutions through corresponding salt/acid/base chambers of IE stack 135. Specifically, the aqueous salt solution enters IE stack 135 as brine stream 111-1 that is divided and directed (e.g., by an input manifold, not shown) into the inlet of each cell's salt flow channel 131, and the aqueous salt solution exits the IE stack 135 by way of an outlet of each cell's salt flow channel 131 (and an outlet manifold, not shown) as reduced-salt stream 111-2. Similarly, the aqueous acid solution enters IE stack 135 as a weak acid stream 112-1 that is directed into the inlet of each cell's acid flow channel 132 and exits the IE stack 135 by way of an outlet of each cell's acid flow channel 132 as acid product stream 112-2. Finally, the aqueous base solution enters IE stack 135 as a weak base stream 113-1 that is directed into the inlet of each cell's base flow channel 133 and exits the IE stack 135 by way of an outlet of each cell's base flow channel 133 as base product stream 113-2.\|[0047] During the electrochemical process the three (salt, acid and base) aqueous solutions are directed through IE stack 135 along parallel flow paths (e.g., in the vertical direction) while a stack voltage VSTACK is applied to electrodes 138+ and 138−. When stack voltage VSTACK is sufficiently strong, the resulting electric field E produces an ionic current across IE stack 135 in a direction perpendicular to the parallel flow paths (e.g., in the horizontal direction). This ionic current causes dissociated salt molecules (i.e., sodium ions (Na+) and chloride ions (Cl−)) to exit brine stream 111-1 in opposite directions (i.e., such that the chloride ions (Cl−) pass through ion exchange filter 138-1 from salt chamber 131 into the acid chamber 132, and the sodium ions (Nat) pass through ion exchange filter 138-2 into base chamber 133). The chloride ions (Cl−) then combine with protons (H+) to form “new” acid molecules (HCl) in the acid solution stream flowing through acid chamber 132, and the sodium ions (Na+) combine with hydroxide ions (OH−) to form “new” base molecules (NaOH) in the base solution stream flowing through base chamber 133. As a result of this electrochemical salt-conversion process, base product stream 113-2 exits each cell's base chamber 133 with a significantly higher concentration of base molecules than weak base stream 113-1 (i.e., the aqueous base solution before it enters IE stack 135). Similarly, acid product stream 112-2 exiting each cell's acid chamber 132 has a higher concentration of acid molecules than that of weak acid stream 112-1. Note that, because salt is converted (consumed) to generate the acid and base molecules, reduced-salt stream 111-2 exiting each cell's salt chamber 131 has a lower salt concentration than inflowing brine stream 111-1.\|[0048] Referring to the lower left portion of FIG. 1, system controller 190 controls the various operations performed by electrochemical reactor 110 by way of operation/control signals 191, and controls the various operations performed by desalination subsystem 160 way of operation/control signals 192 such that at least a portion of the freshwater 115 exiting desalination unit 180 is directed out of system 100 as freshwater output stream 115-OUT. In an embodiment system controller 190 controls the operating state of ED apparatus 130 such that the above-described electrochemical process is performed at a rate that converts/removes a sufficient amount salt from brine stream 111-1 such that reduced-salt stream 111-2 leaving electrochemical reactor 110 has a relatively low (third) salt concentration that is lower than the initial (first) salt concentration of the saltwater feedstock. In some embodiments system controller 190 controls a flow rate of mixture stream 51M into desalination unit 180 using sensor data from sensors configured to measure the flow rate of reduced-salt stream portion 111-21 (i.e., some or all of reduced-salt stream 111-2) from electrochemical reactor 110 into mixing device 170 and using a feedstock flow control device (e.g., pump or valve) to control the associated flow rate of saltwater feedstock stream 51T into mixing device 170. Note that, because the salt concentration of reduced-salt stream 111-2 is lower than the initial (first) salt concentration of saltwater feedstock 51/51T, any non-zero flow rate of reduced-salt stream portion 111-21 into mixing device 170 causes the solution forming mixture stream 51M to have a (fourth) salt concentration that is lower than the initial (first) salt concentration of saltwater feedstock 51/51T. Therefore, although operational and maintenance costs associated with desalination subsystem 160 may be reduced by way of directing all (i.e., the totality of) reduced-salt stream 111-2 from ED apparatus 130 to mixing device 170, beneficial reductions in total system operating costs may be achieved when reduced-salt stream portion 111-21 includes less than all of reduced-salt stream 111-2, and the remaining portion is redirected for other purposes (e.g., reduced-salt stream portion 111-22 may be used in place of or in combination with freshwater portion 115-2 to replenish (make-up) the acid and base solutions stored in buffer tanks 121-2 and 121-3). In some embodiments, system controller 190 is implemented using one or more processors configured to implement a software-based control algorithm that utilizes one of a proportional integral derivative, machine learning and/or artificial intelligence to coordinate the desalination and OAE processes (described below). In some embodiments, controller 190 controls the operations performed by electrochemical reactor 110 to perform additional functions described in co-owned U.S. Pat. No. 11,629,067, cited above.\|[0049] FIG. 2 shows a generalized bipolar electrodialysis (BPED) system (electrochemical reactor) 110A of a type similar to that utilized in some Ocean alkalinity enhancement (OAE) systems. BPED 110A generally includes a fluid buffering system 120A, an ED apparatus 130A, a flow control system 140A and a series of flow lines that are described in additional detail below. Additional details of BPED 110A are provided in U.S. Pat. No. 11,629,067, entitled “OCEAN ALKALINITY SYSTEM AND METHOD FOR CAPTURING ATMOSPHERIC CARBON DIOXIDE”, which is incorporated herein by reference in its entirety.\|[0050] Referring to the upper portion of FIG. 3, fluid buffering system 120A includes an optional salt buffer tank 121A-1 utilized to receive and store brine stream (salt solution) 111-1, an acid buffer tank 121A-2 utilized to store an acid solution 112A, and a base buffer tank 121A-3 utilized to store a base solution 113A. Each buffer tank 121A-1 to 121A-3 can be implemented using a standard 1000 L IBC caged tote tank, where salt buffer tank 121A-1 includes a plastic containment unit 122A-1 having an inflow port 123A-1 operably coupled to receive brine stream 111-1 and an outflow port 124A-1 operably coupled to salt chamber(s) 131 of ion exchange stack 135, acid buffer tank 121A-2 includes a plastic containment unit 122A-2 having an inflow port 123A-21 operably coupled to receive acid product stream portion 112A-21 and an outflow port 124A-2 operably coupled to acid chamber(s) 132 of ion exchange stack 135, and base buffer tank 121A-3 includes a plastic containment unit 122A-3 having an inflow port 123A-31 operably coupled to receive base product stream portion 113A-21 and an outflow port 124A-3 operably coupled to base chamber(s) 133 of ion exchange stack 135. Portions of freshwater output stream 115 generated by desalination unit 180 (shown in FIG. 1) and/or portions of reduced-salt stream 111A-2 may be directed to buffering system 120A and utilized to dilute and maintain acid solution 111A and base solution 113A at suitable levels within buffer tanks 121A-2 and 121A-3.\|[0051] Electrodialysis apparatus 130A includes ion exchange stack 135 and is otherwise configured and operates as described above with reference to FIG. 1 to electrochemical process NaCl (salt) molecules provided in brine stream 111-1 such that Cl-ions pass from salt chamber 131 though ion exchange membrane 134-1 into acid chamber 132 to enhance (i.e., decrease the pH of) acid solution 112A, and such that Nat ions pass from salt chamber 131 though ion exchange membrane 134-2 into base chamber 133 to enhance (i.e., increase the pH of) base solution 113A. Ion exchange stack 135 can be surrounded by a water-tight containment housing (not shown) to facilitate the flow of salt solution 111A through salt chamber(s) 131, the flow of acid solution 112A through acid chamber(s) 132, and the flow of base solution 113A through base chamber(s) 133. Cathode 138A− and anode 138A+ are disposed at opposite ends of ion exchange stack 135 and generate an electric field through the chambers in response to an applied voltage differential provided by a suitable voltage source VS, thereby electrochemically processing the salt, acid and base streams in the manner described herein.\|[0052] Similar to BPEDs utilized in OAE systems, flow control system 140A includes various control elements (e.g., pumps, valves etc.) that are collectively configured to direct streams of the acid and base solutions from buffer tanks 121A-2 and 121A-3 through corresponding chambers 132 and 133 of electrodialysis apparatus 130A and then back to buffer tanks 121A-2 to 121A-3 by way of associated conduits (flow lines). Specifically, weak acid stream 112A-1 exits acid buffer tank 121A-2 and is directed into acid chamber 132A by way of acid inflow line 1501A-2 and a pump 145A-21, and strong acid stream 112A-2 exits acid chamber 132A by way of acid outflow line 152A-2, with a first portion 112A-21 being returned to acid buffer tank 121A-2 by way of optional three-way valve 146A-2 and acid return line 153A-2, and a second portion 112A-22 of strong acid stream 112A-2 being diverted out of BPED 110A, e.g., for system maintenance purposes or commercial sale. Similarly, weak base stream 113A-1 exits base buffer tank 121A-3 and is directed into base chamber 133A by way of base inflow line 151A-3 and a pump 145A-31, a portion 113A-21 of strong base stream 113A-2 exiting base chamber 133A by way of base outflow line 152A-3 is returned to base buffer tank 121A-3 by way of three-way valve 146A-3 and a base return line 153A-3, and a second portion 113A-22 of strong base stream 113A-2 is diverted out of BPED 110A, e.g., for OAE purposes (e.g., as described below with reference to FIG. 5) or for commercial sale.\|[0053] BPED 110A differs from BPEDs typically utilized in OAE systems in that, unlike the acid and base solutions, flow control system 140A does not circulate all of weak salt solution exiting ion exchange stack 135 back to the acid/base buffer tanks. Instead, flow control system 140A is configured to direct brine stream 111-1 into salt chamber(s) 131 and to direct at least a portion 111A-21 of reduced-salt stream 111A-2 from salt chamber(s) 131 to mixing device 170 (shown in FIG. 1). Specifically, brine stream 111A-1 exits (flows from) salt buffer tank 121A-1 by way of outflow port 124A-1 and is directed into salt chamber 131 by way of salt inflow line 151A-1 and a first pump 145A-11, and reduced-salt stream 111A-2 exits salt chamber 131 by way of salt outflow line 152A-1. A valve 146A-1 is controlled by the system controller to direct a first portion 111A-21 of reduced-salt stream 111A-2 to mixing device 170 by way of an optional and an associated flow line 153A-1. A benefit of this arrangement is that, when ED apparatus 130A is operated such that reduced-salt stream 111A-2 has a salt concentration lower than that of the saltwater feedstock, less saltwater feedstock must be pumped to and processed by the desalination subsystem (not shown in FIG. 2), thereby reducing both operating energy and maintenance costs in at least some cases. Flow control system 140A also includes an optional valve 146A-4 that controllable by the system controller to direct a first portion 115-1 of freshwater stream 115 (received from desalination unit 180, see FIG. 1) for use as freshwater output stream 115-OUT, and directs second portion 115-2 of freshwater stream 115 to buffering system 120A (i.e., into one or both of acid buffer tank 121A-2 and base buffer tank 121A-3 to replenish acid/base product diverted from electrochemical reactor 110A for other purposes). Note that valve 146A-1 is also controllable to selectively direct a second portion 111A-22 of reduced-salt stream 111A-2 to fluid buffering system 120A for similar reasons.\|[0054] FIG. 3 shows a portion of a BPED system 110B including an ED apparatus 130B that includes an ion exchange stack 135B, an input manifold 136B-1, an output manifold 136B-2 and an electrolyte solution circulation system 139B. ED apparatus 130B may provide additional details regarding the multiple acid, salt and base chambers described above with reference to ED apparatus 130A (FIG. 2). That is, in some embodiments ED apparatus 130A (FIG. 3) is configured to include the features and details of ED apparatus 130B.\|[0055] Ion exchange stack 135B includes multiple acid chambers 131B-1 to 131B-N, multiple salt chambers 132B-1 to 132B-N and multiple base chambers 133B-1 to 133B-N disposed in a repeating series of cells that are arranged in series between two end chambers 137B-1 and 137B-2. For example, a first cell in the series may include salt chamber 131B-1 disposed between associated acid chamber 132B-1 and associated base chamber 133B-1, and a last cell in the series may include salt chamber 131B-N disposed between associated acid chamber 132B-N and associated base chamber 133B-N. Each of the acid, salt and base chambers of ion exchange stack 135B may function as described above with reference to acid chamber 132, salt chamber 131 and base chamber 133, respectively, to process a corresponding portion of one of the acid, salt and base solution streams directed through ion exchange stack 134B by way of input manifold 136B-1 and output manifold 136B-2. That is, input manifold 136B-1 may split weak acid stream 112B-1 (which is received from an acid buffer tank (not shown) by way of acid inflow line 151B-2) such that corresponding portions of the acid stream pass through each acid chamber 131B-1 to 131B-N. Similarly, input manifold 136B-1 receives brine stream 111-1 by way of salt inflow line 151B-1 and splits brine stream 111-1 into multiple stream portions that are directed through salt chambers 131B-1 to 131B-N, and receives weak base stream 113B-1 from a base buffer tank (not shown) by way of base inflow line 151B-3 and splits weak base stream 113B-1 into multiple stream portions that are directed through base chambers 133B-1 to 133B-N. End chambers 137B-1 and 137B-2 may function to conduct an electrolyte solution indicated by “ES” for purposes described below.\|[0056] Ion exchange stack 135B may include four types of ion permeable membranes that are respectively disposed between adjacent acid, salt, base and end chambers and facilitate the ion transfer process utilized to strengthen the base stream and the salt stream during operation of BPED 110B (i.e., when ion exchange stack 135B receives an electric field generated applying voltage potentials V+ and V− to anode 138B+ and cathode 138B−, respectively). The four types of membranes are indicated in FIG. 3 using the prefixes “A”, “K”, “B” and “F”, where membranes A1 to An are anion exchange membranes, membranes K1 to Kn are cation exchange membranes, membranes B1 to Bn are bipolar membranes, and membranes F1 and F2 are end membranes having characteristics described below. Electrolyte solution circulation system 139B may include a reservoir 139B-0 and flow lines 139B-1 to 139B-3 that function to circulate an electrolyte solution 114B through end chambers 137B-1 and 137B-2. That is, electrolyte solution 114B can be pumped from reservoir 139B-0 along first flow line 139B-1 to first end chamber 137B-1, from end chamber 137B-1 along second flow line 139B-2 to second end chamber 137B-2, and from second end chamber 137B-2 along third flow line 139B-3 to reservoir 139B-0. During operation the electrolyte solution may give up Na+ ions at one end of ion exchange stack 134B and reabsorbs Nat ions at the opposing end of ion exchange stack 135B. In some embodiments, electrolyte solution 114B is implemented using sodium sulfate or a semi conductive solution such as sodium hydroxide.\|[0057] FIG. 4 shows a modified desalination system 100D including an electrochemical reactor 110D and a desalination subsystem 160D.\|[0058] Referring to the lower portion of FIG. 4, electrochemical reactor 110D generally includes a fluid buffering system 120D, an ED apparatus 130D and a flow control system 140D. Fluid buffering system 120D includes an acid buffer tank (ABT) 121D-2 and a base buffer tank (BBT) 121D-3. Acid buffer tank 121D-2 stores an aqueous acid solution formed by a portion 112D-21 of an acid product stream 112D-2 exiting ED apparatus 130D and a portion 115D-21 of freshwater stream 115D exiting desalination subsystem 160D and supplies a relatively weak acid stream 112D-1 to ED apparatus 130D. Base buffer tank 121D-3 stores an aqueous base solution formed by a portion 113D-21 of a base product stream 113D-2 exiting ED apparatus 130D and a portion 115D-22 of freshwater stream 115D exiting desalination subsystem 160D and supplies a relatively weak base stream 113D-1 to ED apparatus 130D. ED apparatus 130D includes an ion exchange stack 135D disposed between electrodes 138D− and 138D+, an input manifold 136D-1 and an output manifold 136D-2, and is configured to receive and electrochemically process brine stream 111D-1, weak acid stream 112D-1 and weak base stream 113D-1 in the manner described above to generate reduced-salt stream 111D-2, acid product stream 112D-2 and base product stream 113D-2. Flow control system 140D includes pipes, pumps (indicated by circled arrows) and valves that are configured to direct the various solution flows between desalination subsystem 160D and electrochemical reactor 110D, and to selectively divert a portion 113D-22 of base product stream 113D-2 and a portion 112D-22 of acid product stream 112D-2 for one or more non-OAE purposes (e.g., for sale to a third party, or for system maintenance or commercial purposes). Flow control system 140D also includes flow control valves 146D-1 and 146D-4. Flow control valve 146D-1 effectively divides freshwater 115D exiting RO unit 180D into a first freshwater stream portion 115D-1 that is directed out of system 100D as freshwater output stream 115D-OUT and a second freshwater stream portion 115D-2 directed to fluid buffering system 120D. Flow control valve 146D-4 effectively divides reduced-salt stream 111D-2 into a first reduced-salt stream portion 111D-21 directed to desalination subsystem 160D and a second reduced-salt stream portion 111D-22 directed to fluid buffering system 120D. As discussed below, the system controller may utilize sensors and other control data to determine the flow amounts (flow rates) of each stream portion 111D-21, 111D-22, 115D-1 and 115D-2, and to adjust the operating states of flow control valves 146D-1 and 146D-4 by way of appropriate control signals to achieve the determined flow amounts.\|[0059] Referring to the upper portion of FIG. 4, desalination subsystem 160D includes a pretreatment unit 165D, a mixing tank (mixing device) 170D and a reverse osmosis system (desalination unit) 180D.\|[0060] Pretreatment unit 165D includes a solids filtering device 166D and a metals/biological removal device 168D that are connected in series such that raw saltwater feedstock 51 must pass through both series-connected filtering devices before being supplied to mixing tank 170D. Each filtering device 166D and 168D utilizes an associated filter to remove targeted contaminants from raw saltwater feedstock 51 (e.g., filtering system 166D utilizes one or more filters 167D that are optimize to remove solid particles from feedstock 51, and filtering system 168D utilizes one or more filters 169D that are optimized to remove metals and/or biologic materials from partially filtered seawater/brine 51T1 received from the first filtering system 166D). The order and number of filtering devices may be different from that shown in FIG. 4. As indicated by the arrows in the upper right portion of FIG. 4, the filtered contaminants (e.g. removed solids, metals and/or biological materials) are removed from the feedstock flow path using known techniques, and the resulting treated (filtered) feedstock solution 51T2 (i.e., the treated saltwater feedstock solution that has passed through both filters 167D and 169D) forms a treated saltwater feedstock stream 51T2 that is passed downstream to mixing tank 170D.\|[0061] Mixing tank 170D is configured to receive reduced-salt stream portion 111D-21 (i.e., some or all of reduced-salt stream 111D-2 exiting ED apparatus 130D) and treated saltwater feedstock stream 51T2 from pretreatment unit 165D. Mixing tank 170D is also configured such that treated saltwater 51T and reduced-salt stream 111D-2 combine (intermix) within the mixing tank 165D to form saltwater/reduced-salt mixture 51M, which is then passed to RO system 180D. Mixing tank 170D is configured to generate mixture stream 51M by combining all of reduced-salt stream portion 111-21 received from electrochemical reactor 110 with a corresponding portion of treated/untreated saltwater feedstock 51T2, which may be controlled by way of a feedstock flow control device 171D in a manner similar to that described above with reference to FIG. 1.\|[0062] RO system 180D receives mixtures stream 51M from mixing tank 170D and utilizes a semi-permeable membrane 181D that prevents the passage of salt molecules, whereby brine stream 111D-1 is formed on one side of membrane 181D and permeate (freshwater) passes through membrane 181D and exit as freshwater stream 115D. Similar to conventional desalination processes, freshwater stream 115D generated RO unit 180D has a suitably low salt concentration (e.g., ≤500 ppm), and brine stream 111-1 comprises an aqueous solution having salt content greater than 50,000 ppm (5%), whereby at least a portion of freshwater stream 115D is suitable for use as freshwater output stream 115D-OUT (i.e., suitable for human consumption and other freshwater uses).\|[0063] Modified desalination system 100D also includes a system controller (not shown) that controls the various operations performed by electrochemical reactor 110D and desalination subsystem 160D way of operation/control signals in the manner described above. In addition, the system controller controls the operating states of flow control valves 146D-1 and 146D-4 in response to sensor data and/or externally supplied data to optimize system operations for reasons set forth above. In some embodiments, flow control valve 146D-4 may be controlled to stop all flow of reduced-salt solution to mixing device 170D, for example, when insufficient clean energy is available and/or electrochemical reactor 110D is shut down. During such periods system 100D may be operated in a manner similar to that implemented by a conventional desalination system.\|[0064] FIG. 5 depicts a system 100E according to another embodiment. In the depicted embodiment, system 100E includes an OAE subsystem (electrochemical reactor) 110E, a seawater desalination subsystem 160E and an enhanced ocean weathering (EOW) subsystem 200, whereby system 100E is sometimes referred to herein as an integrated desalination/OAE/EOW system. However, in some embodiments EOW subsystem 200 may be omitted, whereby system 100E may be referred to as an integrated desalination/OAE system (i.e., by way of including OAE subsystem 110E and seawater desalination subsystem 160E). In other embodiments, seawater desalination subsystem 160E may be omitted (e.g., seawater 51 is pumped directly to OAE subsystem 110E), whereby system 100E may be referred to as a hybrid CDR system for reasons that will become clear below. Therefore, although system 100E is depicted as an integrated desalination/OAE/EOW system, it is understood that FIG. 5 also shows an integrated desalination/OAE system and a hybrid CDR system.\|[0065] Referring to seawater desalination subsystem 160E (lower portion of FIG. 5), seawater 51 is pumped or otherwise drawn from ocean 50 into a pretreatment unit 165E (e.g., a nanofiltration, ultrafiltration, chemical precipitation or other water purification system) that is configured to treat (i.e., remove contaminants from) seawater 51. Treated seawater 51T is then mixed with reduced-salt stream 111E-22 in mixing device 170E to form a treated seawater/reduced-salt mixture solution 51M, and then mixture solution 51M is processed by a desalination unit 180E (e.g., a membrane-based or thermal desalination system) to generate freshwater 115E and a byproduct brine stream 111E-1, thereby providing freshwater output stream 115E. In one embodiment, pretreatment unit 165E is configured to remove hardness related minerals HRM (along with other contaminants) such that a hardness of seawater 51 is reduced before being supplied to mixing device 170E. In some embodiments, as indicated by the dashed-line arrow, the hardness related minerals HRM are supplied to a post-production unit 150E and returned to ocean 50 with the ocean alkalinity product and/or alkaline slurry (both discussed below).\|[0066] OAE subsystem 110E includes a fluid buffering system 120E, an ED apparatus 130E and a flow control system that are configured and operate in the manner described in at least one of the previously described embodiments. ED apparatus 130E converts salt provided in brine stream 111E-1 into acid molecules (e.g., HCl) disposed in an acid product stream 112E-2 and base molecules (e.g., NaOH) disposed in a base product stream 113E-2. Base buffer tank 120E includes an acid buffer tank (ABT) that receives a (first) portion 112E-21 of acid product stream 112E-2 and supplies a weak acid stream to ED apparatus 130E, a base buffer tank (BBT) that receives a (first) portion 113E-21 of base product stream 113E-2 and supplies a weak base stream to ED apparatus 130E, and an optional salt buffer tank (SBT) that receives brine stream 111E-1 from desalination unit 180E and supplied brine stream 111E-1 to ED apparatus 130E. Although not depicted in FIG. 5 for clarity, portions of reduced salt stream 111E-2 and/or freshwater stream 115E may be directed to acid buffer tank (ABT) and base buffer tank (BBT) for the make-up and dilution purposes discussed above.\|[0067] System 100E also includes a post-production unit 150E that selectively utilizes a portion 113E-22 of base product stream 113E-2 to generate an ocean alkalinity product 113E-OUT and selectively utilizes a portion 112E-22 of the acid product stream 112E-2 to generate an alkaline slurry 246, and then supplies (e.g., pumps) the ocean alkalinity product 113E-OUT and the alkaline slurry 246 to the ocean 50 at a designated outfall location 50-1 for OAE purposes (i.e., such that both the fully dissolved base substance in the ocean alkalinity product and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide CO2 and mitigate ocean acidification). In the exemplary embodiment, a portion of post-production unit 150E that is considered part of OAE subsystem 100E includes an acid product tank 127E-2, a base product tank 127E-3, an alkalinity product (ALK PROD) generator 153E and a base delivery subsystem 159E. Acid product tank 127E-2 receives and stores a portion 112E-22 of acid product stream 112E-2, and base product tank 127E-3 receives and stores a portion 113E-22 of base product stream 113E-2. Alkalinity product generation unit 153E is configured to generate an ocean alkalinity product 113E-OUT using a base product stream portion 113E-31, which is received from base product tank 127E-3, such that ocean alkalinity product 113E-OUT includes base molecules (NaOH) that are fully dissolved in a salt solution and has a pH level that is a predetermined amount higher than a pH level of the ocean's seawater 51 (e.g., in a target pH range between 8.0 and 9). In some embodiments, the ocean alkalinity product 113E-OUT is generated using a dilution apparatus configured to operate in the manner described in co-owned and co-pending U.S. Published Patent Application No. US 2024-0336503 A1, entitled “PRODUCTION EFFICIENCY OPTIMIZATION FOR BIPOLAR ELECTRODIALYSIS DEVICE”, which was published on Oct. 10, 2024, and is incorporated herein by reference in its entirety. Post-production unit 150E also includes an enhanced ocean weathering (EOW) subsystem 200 that is configured to generate an alkaline slurry 246 using an acid product stream portion 112E-31, which is received from acid product tank 127E-2, by combining acid product stream portion 112-31 with a coarsely-ground alkaline aggregate (rock) such that a reaction between the alkaline aggregate and the acid molecule both neutralizes the acid molecules and etches/weakens the alkaline aggregate. Enhanced ocean weathering subsystem 200 is described in additional detail below with reference to FIG. 6. Base delivery subsystem 159E is configured and controlled by system controller 190E to supply (e.g., pump) at least one of ocean alkalinity product 113E-OUT and alkaline slurry 246 to ocean 50 at a designated outfall location 50-1.\|[0068] System controller 190E is programmed and otherwise configured to control operations of OAE subsystem 110E by way of control signals 191E, to control operations of desalination subsystem 160E by way of control signals 192E, and configured to control operations of post-production unit 150E by way of control signals 193E and 194E such that one or both of alkalinity product 113E-OUT and alkaline slurry 246 are selectively supplied to ocean 50 in safe and efficient manner. In one embodiment, system controller 190E monitors sensors and other data sources (e.g., via data 195E) and controls base delivery system 159E by way of control signal 194E such that ocean alkalinity product 113E-OUT and alkaline slurry 246 are only supplied to ocean 50 when data 195E indicates that sea life adjacent to outfall location 50-1 will not be endangered by the release of these OAE substances. In another embodiment, system controller 190E may monitor one or more sites that provide input data 195E including spot pricing for the base product and/or acid product generated by electrochemical reactor 110E. Controller 190E may then utilize this input data to determine whether the base and/or acid products should be utilized for OAE/EOW purposes, or whether they should be sold to a third-party buyer. For example, when sufficient low/zero-carbon electricity is available from a power grid to offset the desalination process carbon footprint and the base product spot price is sufficiently high, then the controller 190E may direct the post-production unit 150E (e.g., by way of control signals 191E) to divert a base product portion 113E-220 (e.g., some or all of the second base stream portion 113E-22) for sale to a third-party buyer (i.e., instead of directing the base product to ocean 50 as part of ocean alkalinity product 113E-OUT), whereby proceeds from the sale serve to reduce total operating costs of system 100E. Similarly, the control algorithm implemented by system controller 190E may monitor input data 195E from one or more sites that provide spot pricing for the acid product (e.g., HCl), and utilizes this data to determine whether it is more cost effective to neutralize the acid product (e.g., by way of EOW subsystem 200), or if selling the acid product may produce a greater value (i.e., if the acid product spot price is sufficiently high), in which case the controller 190E may direct the post-production unit 150E to divert an acid product portion 112E-220 (e.g., some or all of the second acid stream portion 112E-22) for sale to a third-party buyer.\|[0069] FIG. 6 shows EOW subsystem 200 of integrated desalination/OAE/EOW system 100E (see FIG. 5) according to an exemplary embodiment. EOW subsystem 200 includes an accelerated ocean weathering reaction apparatus 210, a dosing apparatus 230, a slurry generator 240 and a neutralization controller 280. Accelerated ocean weathering reaction apparatus 210 includes a reaction tank 211 configured to contain a process fluid 215 including a mixture of alkaline aggregate 95 and acid product portion 112E-31 until the acid molecules are neutralized and alkaline aggregate 95 is etched/weakened. In some embodiments, alkaline aggregate 95 may be transported from a quarry or other source by a material delivery vehicle 92 and processed by an optional pre-crusher/grinder 201 before the pre-crushed/ground alkaline aggregate 95-1 is delivered into reaction tank 211 by way of an inlet pipe 203. Dosing apparatus includes one or more dosing pumps 231 that receive acid product portion 112E-31 from acid product tank 127E-2 and is controlled by neutralization controller 280 to inject acid product doses 112E-4 into reaction tank 211 by way of an injector 235. Neutralization controller 280 controls the delivery/injection of alkaline aggregate and acid product into reaction tank 211 by way of monitoring a process fluid pH measurement data pHPF generated by a first sensor S1 disposed inside reaction tank 211 and acid product pH measurement data pHAP generated by a second sensor S2 disposed upstream from acid dosing pump(s) 231. During operation neutralization controller 280 controls the injection rate of acid product doses 112E-4 into reaction tank 211 such that a pH level of process fluid 215 is optimized such that acid molecules are neutralized and alkaline aggregate 95 is etched/weakened at a maximum rate. Neutralized product (i.e., a combination of neutralized acid solution and weakened/etched alkaline aggregate) is passed from reaction tank 211 to slurry generator 240 by way of an outlet pipe 241. Slurry generator 240 is configured to generate alkaline slurry 246 by processing (e.g., crushing/grinding) the etched/weakened alkaline aggregate of neutralized product 215N into fine particles, and then passes alkaline slurry 246 to base delivery subsystem 159E (see FIG. 5). In some embodiments, the accelerated weathering reaction causes the release of one or more metal elements (e.g., Nickel, Cobalt, Aluminum, Magnesium, Potassium and/or Lithium) from the alkaline aggregate and the slurry generator 240 is configured reclaim (i.e., separate and remove) the released metal elements from alkaline slurry 246 using known techniques, whereby system costs may be further reduced/offset by way of commercial sale of the reclaimed metals. In some embodiments, the operation of EOW subsystem 200 is controlled by system controller 190E by way of control signals 193E passed to neutralization controller 280.\|[0070] Referring again to FIG. 5, by configuring post-production unit 150E to implement both alkaline production generator 153E and EOW subsystem 200, system 100E implements a hybrid carbon dioxide removal (CDR) process and a reduced ocean acidification (ROA) process that combines some portions of each of a conventional electrochemical ocean alkalinity enhancement (EOAE) process and a conventional EOW process to achieve combined beneficial results (i.e., CDR/ROA-EOAE and CDR/ROA-EOW) achieved by both conventional processes, but changes other portions of each conventional processes in a way that reduces total operating costs (i.e., in comparison to separately performing the two conventional processes). For example, in one embodiment the hybrid CDR system implements the conventional EOAE process portions related to electrochemically processing salt to generate a base substance (e.g., NaOH) and an acid substance (e.g., HCl) and supplying the base substance to the ocean by way of an ocean alkalinity product, and the hybrid CDR system also implements the conventional EOW process portion related to mining and transporting alkaline aggregate/rock. The changes to the conventional EOAE and EOW processes occur after the acid byproduct is produced and after the alkaline rock is transported, whereby the conventional disposal of the acid byproduct and conventional crushing/grinding of the alkaline rock are replaced with an advanced weathering operation that includes combining alkaline rock and the acid product/substance generated by ED apparatus 130. In the embodiment described above with reference to FIG. 6, the advanced weathering operation involves mixing the acid product portion 112E-31 and alkaline rock/aggregate (e.g., olivine/basalt or other mafics/ultramafics) to produce alkaline slurry 246 with a pH between two and eight. As discussed above, slurry generation may include pre-grinding/crushing and/or post-reaction processing of the alkaline rock, but these optional processes require substantially less externally supplied energy than that required by the conventional crushing/grinding process and therefore costs less to perform than conventional acid disposal and crushing/grinding. During the advanced weathering operation, the acid substance in the acid byproduct reacts with alkaline substances in the alkaline rock, thereby weakening and/or increasing the surface area of the alkaline rock and neutralizing the acid substance. During the advanced weathering operation valuable and/or toxic metal constituents of the alkaline aggregate (Ni, Co, Al, Mg, K, Li, etc.) may be reclaimed from the slurry using known techniques. The advanced weathering process proceeds until the acid substance (e.g., HCl) supplied in the acid byproduct is neutralized, at which point the final alkaline slurry has a pH higher than ambient ocean pH (>7.5). The final alkaline slurry could then be dispersed into the ocean via fixed point (e.g., by way of base delivery subsystem 159E) or released from a moving vessel.\|[0071] Although the invention is primarily described herein in the context of seawater desalination and seawater-based OAE systems/methods, various novel aspects described herein may be beneficially utilized in other systems/methods without departing from the spirit and scope of the invention. For example, the chemical reactor implemented by the present invention may be utilized to electrochemically process a wide variety of salt types to generate corresponding base and acid substances. It will be clear to those skilled in the art that the inventive features of the present invention are applicable to these other embodiments as well, and that all of which are intended to fall within the scope of the present invention.	Family Number\|(116490379)\|116490379\|Object of Invention\|(US20250339810 A1)\|The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|(WO2025230667 A1)\|The invention generally relates to desalination systems/methods that separate saltwater into freshwater and brine and to carbon dioxide removal systems/methods.\|Abstract\|(US20250339810 A1)\|A desalination unit processes saltwater feedstock (e.g., seawater) to generate freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a high-salt brine stream. An optional pretreatment unit removes contaminants from the saltwater feedstock before desalination. An electrochemical reactor converts the brine stream into a reduced-salt stream having a salt content lower than the saltwater feedstock by converting salt molecules contained in the brine stream into acid molecules contained in an acid product stream and base molecules contained in a base product stream. A mixing device combines the reduced-salt stream with the saltwater feedstock before the resulting mixture solution is delivered to the desalination unit for desalination. The base product stream leaving the electrochemical reactor may be used for ocean alkalinity enhancement (OAE), and the acid product stream may be used to reduce energy costs associated with crushing/grinding alkaline rock in an enhanced ocean weathering (EOW) process.\|(WO2025230667 A1)\|A desalination unit processes saltwater feedstock (e.g., seawater) to generate freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a high-salt brine stream. An optional pretreatment unit removes contaminants from the saltwater feedstock before desalination. An electrochemical reactor converts the brine stream into a reduced-salt stream having a salt content lower than the saltwater feedstock by converting salt molecules contained in the brine stream into acid molecules contained in an acid product stream and base molecules contained in a base product stream. A mixing device combines the reduced-salt stream with the saltwater feedstock before the resulting mixture solution is delivered to the desalination unit for desalination. The base product stream leaving the electrochemical reactor may be used for ocean alkalinity enhancement (OAE), and the acid product stream may be used to reduce energy costs associated with crushing/grinding alkaline rock in an enhanced ocean weathering (EOW) process.\|Independent Claims\|(US20250339810 A1)\| (...) A hybrid carbon dioxide removal (CDR) system comprising: (...) a base delivery subsystem configured to supply the ocean alkalinity product and the alkaline slurry to an ocean such that both the fully dissolved base substance and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidification.\|(WO2025230667 A1)\|16. A hybrid carbon dioxide removal ( CDR) system comprising : an ocean alkalinity enhancement ( OAE ) subsystem including an electrodialysis device configured (...) alkaline slurry to an ocean such that both the fully dissolved base substance and the etched/weakened alkaline aggregate capture/reduce atmospheric carbon dioxide and mitigate ocean acidi fication .\|	Chemical engineering\|Environmental technology	B01D-053/14/75\|B01D-053/14/93\|B01D-061/02/5\|B01D-061/04\|B01D-061/42/2\|B01D-061/46\|B01D-061/58\|B01D-2252/1035\|B01D-2257/504\|B01D-2258/06\|B01D-2311/04\|B01D-2311/08\|B01D-2311/12\|B01D-2311/2673\|C02F-001/00/8\|C02F-001/04\|C02F-001/04/8\|C02F-001/20\|C02F-001/44/1\|C02F-001/469/3\|C02F-001/469/5\|C02F-2103/08\|C02F-2201/46115\|C02F-2209/06\|Y02A-020/124		B01D-053/14/75\|B01D-053/14/93\|B01D-061/02/5\|B01D-061/04\|B01D-061/42/2\|B01D-061/46\|B01D-061/58\|B01D-2252/1035\|B01D-2257/504\|B01D-2258/06\|B01D-2311/04\|B01D-2311/08\|B01D-2311/12\|B01D-2311/2673\|C02F-001/00/8\|C02F-001/04\|C02F-001/04/8\|C02F-001/20\|C02F-001/44/1\|C02F-001/469/3\|C02F-001/469/5\|C02F-2103/08\|C02F-2201/46115\|C02F-2209/06\|Y02A-020/124	B01D-053/14\|B01D-061/02\|B01D-061/46\|B01D-061/58\|C02F-001/00\|C02F-001/04\|C02F-001/44\|C02F-001/469\|C02F-103/08	B01D-053/14\|B01D-061/02\|B01D-061/46\|B01D-061/58\|C02F-001/00\|C02F-001/04\|C02F-001/44\|C02F-001/469\|C02F-103/08					US11629067\|US20190270660\|CN108623050B\|US20160002082\|CA2834163\|US9382135\|EP1809408\|EP2070583\|US20240336503\|US11629067	US11629067 104545208 WHO=Examiner SELF=Y CAT=I\|US20190270660 85893353 WHO=Examiner SELF=N CAT=I\|CN108623050B 81572078 WHO=Examiner SELF=N CAT=I\|US20160002082 67332528 WHO=Examiner SELF=N CAT=I\|CA2834163 61327814 WHO=Examiner SELF=N CAT=I\|US9382135 44912531 WHO=Examiner SELF=N CAT=I\|EP1809408 61956018 WHO=Examiner SELF=N CAT=I\|EP2070583 1733629 WHO=Examiner SELF=N CAT=I\|US20240336503 111695438 WHO=Applicant SELF=Y\|US11629067 104545208 WHO=Applicant SELF=Y		US11629067; CA2834163; EP1809408; US20160002082; US9382135; EP2070583; CN108623050B; US20190270660; XP026472485; XP093163063; US11629067; US20240336503\|	\|(WO2025/230667)\|International Search Report [Examiner]\|-HOUSE K Z ET AL: "Electrochemical acceleration of chemical weathering for carbon capture and sequestration", ENERGY PROCEDIA, ELSEVIER, NL, vol. 1, no. 1, 1 February 2009 (2009-02-01), pages 4953 - 4960, XP026472485, ISSN: 1876-6102, [retrieved on 20090201], DOI: 10.1016/J.EGYPRO.2009.02.327\|-KURT ZENZ HOUSE: "Electrochemical Acceleration of Chemical Weathering as an Energetically Feasible Approach to Mitigating Anthropogenic Climate Change", ENVIRONMENTAL SCIENCE & TECHNOLOGY, vol. 41, no. 24, 1 December 2007 (2007-12-01), US, pages 8464 - 8470, XP093163063, ISSN: 0013-936X, DOI: 10.1021/es0701816\|-SMITH P ET AL.: "Biophysical and economic limits to negative CO emissions", NAT. CLIM. CHANG., vol. 6, 2016, pages 42 - 50\|	PENDING	(US20250339810)\|PENDING\|(WO2025/230667)\|PENDING	ALIVE	(US20250339810)\|ALIVE\|(WO2025/230667)\|ALIVE	(US20250339810)\|LEGAL DETAILS FOR US20250339810\|Actual or expected expiration date=2045-03-27\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-03-27\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19092576\|Application date=2025-03-27\|Standardized application number=2025US-19092576\|Event publication date=2025-03-27\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:CENTRAL, DOCKET\|Event publication date=2025-03-27\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=OPAP\|Event publication date=2025-03-27\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: EBB-009\|Event publication date=2025-03-27\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 22888\|Event publication date=2025-03-27\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2025-03-27\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2025-03-27\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2025-03-27\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2025-04-28\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2025-04-29\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2025-05-05\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2025-05-23\|Event code=US/DKNC\|Event indicator=Pos\|Event group=Examination events\|Docketed New Case - Ready for Examination\|Event publication date=2025-05-23\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2025-08-29\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2025-11-06\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20250339810\|Publication stage code=A1\|Publication date=2025-11-06\|Standardized publication number=US20250339810\|Event publication date=2025-11-06\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|(WO2025/230667)\|LEGAL DETAILS FOR WO2025/230667\|Actual or expected expiration date=2027-11-02\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-04-02\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2025/022798\|Application date=2025-04-02\|Standardized application number=2025WO-US22798\|Event publication date=2025-11-06\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/230667\|Publication stage code=A1\|Publication date=2025-11-06\|Standardized publication number=WO2025230667\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2045-04-02\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP25721408\|Event publication date=2025-12-17\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP	(WO2025/230667)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/230667)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/230667)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/230667)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/230667)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UY, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(US20250339810)\|US\|(WO2025/230667)\|WO; EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcPZ7F88luobU0Gd4JhdgzD3JjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023106361&ekey=1902&xpn=US20250339810&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19092576/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=KfuhNexKo8%252BlQJXmNbX5EsRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2025/230667)\|US\|(US20250339810)\|US	(WO2025/230667)\|NAME=EBB CARBON, INC. 111 S. Maple Avenue South San Francisco, California 94080 , COUNTRY=US\|(US20250339810)\|NAME=Ebb Carbon, Inc. , CITY=South San Francisco , STATE=CA , COUNTRY=US , ATYP=US Company	(WO2025/230667)\|US	(WO2025/230667)\|NAME=BEVER, Patrick Bever, Hoffman & Harms, LLP 18486 Spring Valley Drive Grass Valley, California 94945 , POSTCODE=94945 , COUNTRY=US	(US20250339810)\|US; US\|(WO2025/230667)\|US; US	(US20250339810)\|NAME=Loretz Jeremy, CITY=Burlingame, STATE=CA , COUNTRY=US \|NAME=Pelman Todd, CITY=Moss Beach, STATE=CA , COUNTRY=US\|(WO2025/230667)\|NAME=LORETZ, Jeremy 1207 Floribunda Avenue, #2 Burlingame, California 94010, POSTCODE=94010, COUNTRY=US \|NAME=PELMAN, Todd 931 Wave Avenue Moss Beach, California 94038, POSTCODE=94038, COUNTRY=US	(WO2025/230667)\|6\|(US20250339810)\|6	3	2					(US20250339810)\|Number of Claims: NCL=20\|Number of Drawings: NDR=6\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1,8,16\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|\|(WO2025/230667)\|Number of Claims: NCL=20\|Extended kind: EXTK=x\|	(US20250339810)\|Provisional Appl: US63/641,910 FDD=2024-05-02 [2024US-63641910]\|Provisional Appl: US63/716,029 FDD=2024-11-04 [2024US-63716029]	(US20250339810)\|ENGLISH (ENG)	(US20250339810)\|Patent\|(WO2025230667)\|Patent	Titre: (US20250339810)\|Integrated Ocean Alkalinity Enhancement And Seawater Desalination Résumé: (US20250339810)\|A desalination unit processes saltwater feedstock (e.g., seawater) to generate freshwater (i.e., water suitable for human consumption, irrigation, or industrial uses) and a high-salt brine stream. An optional pretreatment unit removes contaminants from the saltwater feedstock before desalination. An electrochemical reactor converts the brine stream into a reduced-salt stream having a salt content lower than the saltwater feedstock by converting salt molecules contained in the brine stream into acid molecules contained in an acid product stream and base molecules contained in a base product stream. A mixing device combines the reduced-salt stream with the saltwater feedstock before the resulting mixture solution is delivered to the desalination unit for desalination. The base product stream leaving the electrochemical reactor may be used for ocean alkalinity enhancement (OAE), and the acid product stream may be used to reduce energy costs associated with crushing/grinding alkaline rock in an enhanced ocean weathering (EOW) process.	32	Abstract	gpt-4o-mini	uncertain	The article discusses ocean alkalinity enhancement and desalination, which may relate to enhanced weathering, but the focus is primarily on desalination and not explicitly on CO₂ capture or mineral carbonation.
34	US63/391,662P\|WOUS2023/070710\|IDP00202501664	WOUS2023/070710\|IDP00202501664\|EP23843926\|TW112127364	ID2025/07231\|EP4558651\|TW202417649\|WO2024/020548\|WO2024/020548	108265090	WO2024/020548 A3 2024-04-11 [WO202420548]\|WO2024/020548 A2 2024-01-25 [WO202420548]\|ID2025/07231 A 2025-06-02 [ID202507231]\|EP4558651 A2 2025-05-28 [EP4558651]\|TW202417649 A 2024-05-01 [TW202417649]	2022-07-22\|2023-07-21	2023-07-21\|2023-07-21\|2023-07-21\|2023-07-21	2025-06-02\|2025-05-28\|2024-05-01\|2024-04-11\|2024-01-25		(EP4558651)\|2043-07-21\|(WO2024/020548)\|2026-01-22\|(ID2025/07231)\|2043-07-21\|(TW202417649)\|2043-07-21	(EP4558651)\|Methods for obtaining carbon neutral or carbon negative metals from plants, and related compositions	(EP4558651)\|Provided are methods of extracting metals from rocks and sequestering carbon dioxide. In some embodiments, provided are methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. Provided are also compositions, including metal compositions produced by the methods herein.	METALPLANT PUBLIC BENEFIT\|METOPRON CHARITY	(EP4558651)\|Metalplant Public Benefit Corporation ([US])\|(WO2024/020548)\|METALPLANT PUBLIC BENEFIT CORPORATION ([US])\|(WO2024/020548)\|METALPLANT PUBLIC BENEFIT CORPORATION ([US])\|(ID2025/07231)\|METALPLANT PUBLIC BENEFIT CORPORATION\|(TW202417649)\|METALPLANT PUBLIC BENEFIT CORPORATION ([US])	MATZNER ERIC JASON\|WASSERSON LAURA R	(EP4558651)\|MATZNER, Eric Jason\|WASSERSON, Laura R.	(EP4558651)\|J A Kemp LLP ([GB])\|Reg. Nb: 101669666\|(WO2024/020548)\|ROBERTS, Emily Jane et al. ([US])\|(ID2025/07231)\|Marolita Setiati\|(TW202417649)\|CHEN, CHANG-WEN\|CHANG, CHE LUN\|LO, WEN-MIAO	(WO2024/020548)\|Accordingly, there exists a need in the art for cost-effective methods to remove carbon dioxide from the atmosphere at a gigatonne scale while minimizing the negative impacts on the environment.\|Phytomining refers to the use of hyperaccumulator plant species to concentrate metals from soils and subsequently processing the hyperaccumulator biomass to generate useful metal products.\|	(WO2024/020548)\|1. A method, comprising: mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium, and at least 0.1% each by weight of one or more metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; subjecting the weatherable rock-enriched soil to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process, wherein the chemical weathering process releases the one or more metals; and growing one or more metal hyperaccumulator plant in the weatherable rock-enriched soil, wherein each of the metal hyperaccumulator plants is a hyperaccumulator of at least one of the one or more metals released from the weatherable rock.\|25. A processed nickel composition comprising substantially pure nickel, and one or more of the following (i)-(v):(i) precipitated gypsum; (ii) one or more low weight carboxylic acids; (iii) one or more Ni-containing compounds selected from the group consisting of NiO, Ni(0H)2, nickel sulfides, nickel hydroxides, nickel oxalate, and nickel sulfate; or (iv) one or more carbonates selected from the group consisting of K2CO3, CaCCh, K2Ca(CO3)2. \|26. A nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following (i)-(v):(i) one or more elements selected from the group consisting of Ca, Fe, K, Mg, P, C, H, N, and O; (ii) one or more carbonates selected from the group consisting of K2CO3, CaCCh, K2Ca(CO3)2; (iii) plant cells; (iv) hydroxyapatite or oxy-hydroxyapatite; or (v) one or more oxides selected from the group consisting of NiO, CaO, MgO, and MgNiO2. \|27. A method for sequestering carbon dioxide, comprising: providing a weatherable rock comprising a metal; subjecting the weatherable rock to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide by converting carbon dioxide to bicarbonate or carbonate; and extracting and processing the released metal to provide a metal-enriched composition.\|	(WO2024/020548)\|Provided are methods of extracting metals from rocks and sequestering carbon dioxide. In some embodiments, provided are methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide.\|	(EP4558651)\|CARBON NEGATIVE METAL(100,1)\|OBTAINING CARBON NEUTRAL(100,1)\|PLANT(100,1)\|\|(WO2024/020548)\|SEQUESTERING CARBON DIOXIDE(100,2)\|CARBON NEGATIVE METAL(100,1)\|OBTAINING CARBON NEUTRAL(100,1)\|PLANT(100,1)\|METAL EXTRACTION(72,2)\|ULTRAMAFIC ROCK(62,1)\|ROCK(45,1)\|CARBON DIOXIDE(41,2)\|\|(WO2024/020548)\|SEQUESTERING CARBON DIOXIDE(100,2)\|CARBON NEGATIVE METAL(100,1)\|OBTAINING CARBON NEUTRAL(100,1)\|PLANT(100,1)\|METAL EXTRACTION(72,2)\|ULTRAMAFIC ROCK(62,1)\|ROCK(45,1)\|CARBON DIOXIDE(41,2)\|	(WO2024/020548)\|CLAIMS \|What is claimed is: \|1. A method, comprising: mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium, and at least 0.1% each by weight of one or more metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; subjecting the weatherable rock-enriched soil to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process, wherein the chemical weathering process releases the one or more metals; and growing one or more metal hyperaccumulator plant in the weatherable rock-enriched soil, wherein each of the metal hyperaccumulator plants is a hyperaccumulator of at least one of the one or more metals released from the weatherable rock.\|2. The method of claim 1, further comprising: harvesting the one or more metal hyperaccumulator plant; and processing the one or more harvested metal hyperaccumulator plant to provide one or more substantially pure metal.\|3. The method of claim 1 or 2, wherein the at least one metal comprises nickel, cobalt, chromium, or a combination thereof.\|4. The method of claim 2 or 3, wherein the processing of the harvested metal hyperaccumulator plants comprises: ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash comprising at least 5% of the one or more metal by weight; and refining the metal-enriched ash composition to provide one or more substantially pure metal.\|5. The method of any one of claims 1 to 4, wherein Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock- enriched soil while the metal hyperaccumulator plant is growing.\|6. The method of any one of claims 1 to 5, wherein at least 10 tonnes of carbon dioxide are sequestered for every tonne of metal that is produced.\|7. The method of any one of claims 1 to 6, wherein the weatherable rock comprises ultramafic or mafic rock containing trace levels of the metal.\|8. The method of any one of claims 1 to 7, wherein the weatherable rock comprises serpentine.\|9. The method of any one of claims 1 to 8, wherein the weatherable rock comprises serpentinite.\|10. The method of any one of claims 1 to 9, further comprising mining the weatherable rock.\|11. The method of any one of claims 1 to 10, further comprising transporting the mined weatherable rock from a mining location to a grinding location.\|12. The method of any one of claims 1 to 11, wherein mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock.\|13. The method of any one of claims 1 to 12, wherein the particulate weatherable rock composition has a particle size between 1 pm and 10 cm.\|14. The method of any one of claims 1 to 13, wherein the weatherable rock-enriched soil comprises between 10% and 100% particulate weatherable rock composition by weight.\|15. The method of any one of claims 1 to 14, wherein the metal hyperaccumulator plant is a plant belonging to the genus Odontarrhena.\|16. The method of any one of claims 1 to 15, wherein the metal hyperaccumulator plant is grown inside of a greenhouse.\|17. The method of any one of claims 1 to 16, wherein growing a metal hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil.\|18. The method of any one of claims 1 to 17, wherein the pH of the weatherable rock- enriched soil is at least 7.\|19. The method of any one of claims 4 to 18, wherein the ashing of the harvested metal hyperaccumulator plant comprises: drying the metal hyperaccumulator plant to provide a dried biomass composition; crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a metal-enriched ash composition.\|20. The method of claim 2, wherein the processing of the harvested metal hyperaccumulator plant comprises: directly leaching the harvested metal hyperaccumulator plant using sulfuric acid to provide an acid leachate; purifying the acid leachate using column chromatography to provide a Ni-enriched acid leachate; and processing the Ni-enhanced acid leachate to provide a substantially pure nickel.\|21. The method of claim 3, wherein the at least one metal is nickel, and wherein refining the metal-enriched ash composition comprises: leaching the metal-enriched ash composition to provide a leachate; recovering nickel from the leachate using solvent extraction or an ion exchange resin to obtain a recovered nickel composition; and purifying the recovered nickel composition using electrowinning to obtain a substantially pure nickel.\|22. The method of claim 3, wherein the at least one metal is nickel, and wherein refining the metal-enriched ash composition comprises: acid leaching the metal-enriched ash composition to provide an acid leachate; neutralizing the acid leachate with Ca(OH)2 to provide a first treated leachate; adding NaF to the neutralized leachate to provide a second treated leachate; adding ammonium sulfate to the second treated leachate to provide a third treated leachate; drying the third treated leachate to provide ammonium Ni sulfate hexahydrate (ANSH); and processing the ANSH to obtain a substantially pure nickel.\|23. The method of any one of claims 1 to 22, further comprising quantifying the amount of carbon dioxide that is released or sequestered in any one of steps of the method.\|24. Nickel metal prepared according to the method of any one of claims 1 to 23.\|25. A processed nickel composition comprising substantially pure nickel, and one or more of the following (i)-(v):\|(i) precipitated gypsum; \|(ii) one or more low weight carboxylic acids; \|(iii) one or more Ni-containing compounds selected from the group consisting of NiO, Ni(0H)2, nickel sulfides, nickel hydroxides, nickel oxalate, and nickel sulfate; or \|(iv) one or more carbonates selected from the group consisting of K2CO3, CaCCh, K2Ca(CO3)2. \|26. A nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following (i)-(v):\|(i) one or more elements selected from the group consisting of Ca, Fe, K, Mg, P, C, H, N, and O; \|(ii) one or more carbonates selected from the group consisting of K2CO3, CaCCh, K2Ca(CO3)2; \|(iii) plant cells; \|(iv) hydroxyapatite or oxy-hydroxyapatite; or \|(v) one or more oxides selected from the group consisting of NiO, CaO, MgO, and MgNiO2. \|27. A method for sequestering carbon dioxide, comprising: providing a weatherable rock comprising a metal; subjecting the weatherable rock to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide by converting carbon dioxide to bicarbonate or carbonate; and extracting and processing the released metal to provide a metal-enriched composition.\|28. The method of claim 27, wherein: the subjecting of the weatherable rock comprises growing a metal hyperaccumulator plant in the weatherable rock; and the extracting and the processing of the released metal comprises growing a metal hyperaccumulator plant in the weatherable rock.	(WO2024/020548)\| METHODS FOR OBTAINING CARBON NEUTRAL OR CARBON NEGATIVE METALS FROM PLANTS, AND RELATED COMPOSITIONS \|CROSS-REFERENCE TO RELATED APPLICATIONS \|[0001] This application claims priority to and benefit of U.S. Provisional Application Serial No. 63/391,662, filed July 22, 2022, which is incorporated by reference in its entirety. \|FIELD \|[0002] The present disclosure relates generally to methods of extracting metals from rocks and sequestering carbon dioxide, and more specifically to methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. \|BACKGROUND \|[0003] Carbon dioxide is the dominant greenhouse gas released by human activities and the major contributor to global warming. Carbon sequestration is the process of capturing and storing atmospheric carbon dioxide. It is the only approach that humans can use to actively reduce the amount of carbon dioxide in the atmosphere. Currently, two main types of carbon sequestration are geologic carbon sequestration and biologic carbon sequestration. Current methods for sequestering carbon dioxide, such as underground sequestration, generally face problems related to economic viability, carbon dioxide leakage, and potential contamination of groundwater. Accordingly, there exists a need in the art for cost-effective methods to remove carbon dioxide from the atmosphere at a gigatonne scale while minimizing the negative impacts on the environment. \|BRIEF SUMMARY \|[0004] In some aspects, provided herein are methods and systems that combine enhanced weathering and phytomining to not only sequester carbon dioxide but also extract metals from surrounding soil. Enhanced weathering, which includes terrestrial enhanced weathering and oceanic enhanced weathering, is weathering accelerated by spreading finely ground silicate rock onto surfaces. This helps to accelerate chemical reactions between rocks, water and air. Phytomining refers to the use of hyperaccumulator plant species to concentrate metals from soils and subsequently processing the hyperaccumulator biomass to generate useful metal products. Hyperaccumulators are rare plants that draw up metal from the soil on which they grow, and accumulate high levels of metals in their biomass.\|[0005] In some embodiments, the metals may comprise nickel, cobalt, chromium or any combination thereof. In some embodiments, the methods and systems provided sequester carbon dioxide through a chemical weathering process that results in the release of Mg2+ ions. In some embodiments, the metals are phytomined from serpentinite. Serpentinite is a rock comprising one or more of the serpentine group minerals. Minerals in this group are rich in magnesium and iron. Serpentinite has been called serpentine or serpentine rock, particularly in older geographical texts and in wider cultural settings. In some embodiments, serpentinite is a rock comprising one or more of the serpentine group minerals. In some embodiments, serpentinite is a rock comprising one or more minerals having the chemical formula D3[Si2Os](OH)4, wherein D is selected from the group consisting of Mg, Fe, Ni, Mn, Al, and Zn. In some embodiments, serpentinite is a rock comprising one or more mineral selected from the group consisting of amesite, antigorite, berthierine, brindleyite, caryopilite, chrysotile, cronstedtite, fraipontite, guidottiite, kellyite, lizardite, nepouite, and pecoraite. \|[0006] In some embodiments, the methods and systems provided utilize plant species that are tolerant to soils having high metal contents. In some embodiments, the plants are tolerant of high pH soils. In some embodiments, the plants are tolerant of low nutrient soils. In some embodiments, the plants are hyperaccumulators of nickel. In some variations, provided is a method comprising transporting weatherable rock from a quarry, using mechanical activation to grind the weatherable rock to particles to increase reactive mineral surface area, dispersing the weatherable rock particles into the soil within a plot of land, planting nickel hyperaccumulating plants onto the plot of land to capture the nickel released from the weatherable rock during chemical weathering. In some embodiments, the presence of the nickel hyperaccumulating plants accelerates the chemical weathering of the weatherable rock. In some embodiments, the nickel hyperaccumulating plants may be harvested and further processed to yield a purified nickel composition. In some embodiments, the weatherable rock is ground to a particle size suitable to optimize both the rate of chemical weathering and the rate of nickel accumulation in the hyperaccumulating plant. In some embodiments, grinding the rock to particles comprises grinding the rock to a size of between about 1 pm and about 10 cm. In some variations of the foregoing, the weatherable rock comprises serpentine. In some variations of the foregoing, the weatherable rock comprises serpentinite. \|[0007] In some embodiments, the nickel may be nickel metal in oxidation state 0, or any suitable nickel salts and nickel complexes, such as Ni2+ salts. In some variations, the nickel is a Ni2+ salt or complex. In some embodiments, the nickel may be in an oxidation state of -1, 0, 1, 2, 3, or 4, or any combination thereof. \|[0008] In some variations, the weatherable rock may be obtained from the tailings, waste, or overburden from traditional nickel mines. In some embodiments, the weatherable rock comprises serpentine. In some embodiments, the nickel hyperaccumulating plants are directly irrigated. In some embodiments, the irrigation is accomplished using a continuous irrigation system. In some embodiments, the irrigation is accomplished using an automated irrigation system. \|[0009] In some variations, the methods and systems employ hyperaccumulator plants that are capable of growing in high and even pure levels of serpentine and that are be able to survive and accelerate the weathering rate of the serpentine minerals, especially when fertilized and irrigated. \|[0010] In one aspect, provided is a method for obtaining nickel metal, comprising mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium, and at least 0.1% by weight of nickel to provide a particulate weatherable rock composition, combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil, harvesting the nickel hyperaccumulator plant, and processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel. \|[0011] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash comprising at least 5% nickel by weight, and refining the nickel-enriched ash composition to provide a substantially pure nickel. \|[0012] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises heat treating the harvested nickel hyperaccumulator plant to provide a nickel- enriched ash comprising at least 5% nickel by weight, and refining the nickel-enriched ash composition to provide a substantially pure nickel. \|[0013] In certain embodiments, Mg2+ is leached from the weatherable rock-enriched soil at a rate faster than the observed rate of stationary ultramafic minerals, or minerals without plants growing in them. In certain embodiments, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the nickel hyperaccumulator plant is growing. \|[0014] In other variations, the method may be employed for obtaining one or more metals, including nickel, cobalt, chromium or any combination thereof. In variations where a plurality of metals are obtained, multiple hyperaccumulator plants suitable for harvesting the metals are employed in the process. For example, in some variations of the methods, a nickel hyperaccumulator plant and a cobalt hyperaccumulator plant are used in the weatherable rock-enriched soil to harvest a combination of nickel and cobalt. \|[0015] In some embodiments, at least 10 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. \|[0016] In some embodiments, the weatherable rock comprises ultramafic rock. In some embodiments, the weatherable rock comprises mafic rock. In some embodiments, the weatherable rock comprises less than about 55% silica by weight. In some embodiments, the weatherable rock comprises less than about 45% silica by weight. In some embodiments, the weatherable rock comprises between about 45% and about 55% silica by weight. In some embodiments the weatherable rock comprises one or more minerals selected from the serpentine group. In some embodiments, the weatherable rock comprises olivine. In some embodiments, the weatherable rock comprises serpentinite. In some embodiments, the weatherable rock comprises gabbro or basalt, or a combination. In some embodiments, the weatherable rock comprises a combination of mafic rocks or minerals. \|[0017] In some embodiments, the method comprises mining the weatherable rock. In some embodiments, the method comprises transporting the mined weatherable rock from a mining location to a grinding location. In some embodiments, the method comprises mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock. \|[0018] In some embodiments, the particulate weatherable rock composition has a particle size between 1 pm and 10 cm. In some embodiments, the weatherable rock-enriched soil comprises between 10% and 100% particulate weatherable rock composition by weight. \|[0019] In some embodiments, the nickel hyperaccumulator plant is a plant belonging to the genus Odontarrhena. In some embodiments, the nickel hyperaccumulator plant is grown inside of a greenhouse. In some embodiments, the nickel hyperaccumulator plant is grown under polyethylene film (e.g., a polytunnel). \|[0020] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil. In some embodiments, the pH of the weatherable rock-enriched soil is at least 7. In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises intermittently irrigating the weatherable rock-enriched soil. \|[0021] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises fertilizing the plant. In some embodiments, nitrogen, phosphorus, and potassium (NPK) fertilizers are used to fertilize the plant. In some embodiments, calcium is added to the soil. In some embodiments, boron is used to stimulate flowering in the plant. In some embodiments, soil analysis is used to determine which nutrients are lacking in the soil. In some such embodiments, fertilizer is used to provide the plant with one or more of the nutrients that are determined as lacking in the soil. In some embodiments, exogenous additives are used to increase the available levels of metals in the soil. In some embodiments the exogenous additive comprises citric acid. In some embodiments, potassium is added to the soil. In some embodiments, sulphur-containing compounds are added to the soil. \|[0022] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprises drying the nickel hyperaccumulator plant to provide a dried biomass composition, crushing the dried biomass composition to provide a crushed biomass composition, and burning the crushed biomass composition to provide a nickel-enriched ash composition. \|[0023] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises directly leaching the harvested nickel hyperaccumulator plant using sulfuric acid to provide an acid leachate; purifying the acid leachate using column chromatography to provide a Ni-enriched acid leachate; and further processing the Ni-enhanced acid leachate to provide a substantially pure nickel. \|[0024] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises leaching the nickel-enriched ash composition to provide a leachate; recovering nickel from the leachate using solvent extraction or an ion exchange resin to obtain a recovered nickel composition; and purifying the recovered nickel composition using electrowinning to obtain a substantially pure nickel. \|[0025] It should be understood that, in other variations, the embodiments of the method described above for harvesting nickel may be modified to harvest one or more other metals, such as cobalt and chromium, or any combinations of such metals. \|[0026] In some embodiments, refining the nickel-enriched ash composition comprises: acid leaching the nickel-enriched ash composition to provide an acid leachate; neutralizing the acid leachate with Ca(OH)2 to provide a first treated leachate; adding NaF to the neutralized leachate to provide a second treated leachate; adding ammonium sulfate to the second treated leachate to provide a third treated leachate; drying the third treated leachate to provide ammonium Ni sulfate hexahydrate (ANSH); and processing the ANSH to obtain a substantially pure nickel. \|[0027] In some embodiments, the method further comprises quantifying the amount of carbon dioxide that is released or sequestered in one or more steps of the method. \|[0028] In another aspect, provided is nickel metal prepared according to any of the foregoing methods. \|[0029] In another aspect, provided is a processed nickel composition comprising substantially pure nickel, and one or more of the following: (i) precipitated gypsum, (ii) one or more low weight carboxylic acids, (iii) one or more Ni-containing compounds selected from the group consisting of NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, nickel oxalate, and nickel sulfate, or (v) one or more carbonates selected from the group consisting of K2CO3, CaCO3, K2Ca(CO3)2. \|[0030] In another aspect, provided is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: (i) one or more elements selected from the group consisting of Ca, Fe, K, Mg, P, C, H, N, and O, (ii) one or more carbonates selected from the group consisting of K2CO3, CaCO3, K2Ca(CO3)2, (iii) plant cells, (iv) hydroxyapatite or oxyhydroxyapatite, or (v) one or more oxides selected from the group consisting of NiO, CaO, MgO, and MgNiO2.\|[0031] In yet other aspects, provided is a metal-enriched ash obtained by any of the methods described herein. In some variations, the metal is nickel, cobalt, or chromium, or a combination thereof. \|DESCRIPTION OF THE FIGURES \|[0032] The present application can be understood by reference to the following description taken in conjunction with the accompanying figures. \|[0033] FIG. 1 depicts an exemplary process for obtaining metal using weatherable rock and phytomining. \|[0034] FIG. 2 depicts the different growing conditions employed in the assessment of weathering rates for different soil and plant configurations. \|[0035] FIG. 3 depicts the total amount of magnesium leached under each of the conditions of FIG. 2 over the course of 4 months. \|[0036] FIGS. 4 depicts a diagram of an exemplary field- scale randomized complete block design used to investigate the synergistic combination of nickel phytomining and enhanced weathering. \|[0037] FIG. 5 depicts the pH analysis of topsoils for five application rates approximately eight months after crushed serpentinite rock was applied. \|[0038] FIG. 6 depicts the electrical conductivity analysis of topsoils for five application rates approximately eight months after crushed serpentinite rock was applied. \|[0039] FIG. 7 depicts the amount of nickel in the shoot tissues of hyperaccumulator plants grown on soils treated with eight different application rates of serpentinite rock. \|[0040] FIG. 8 depicts the results from a time-series analysis of topsoil Ni concentrations for five application rates using a Mehlich 1 reagent. \|[0041] FIGS. 9 and 10 depicts the results of statistical analysis of the pH of the soil with respect to application rate and sampling time, respectively. \|[0042] FIGS. 11 and 12 depicts the results of statistical analysis of the electrical conductivity of the soil with respect to application rate and sampling time, respectively.\|[0043] FIGS. 13 and 14 depicts the results of statistical analysis of the ammonium acetate extractable nickel content of the soil with respect to application rate and sampling time, respectively. \|[0044] FIG. 15 depicts the results of statistical analysis of the ammonium acetate extractable magnesium content of the with respect to application rate and sampling time. \|[0045] FIG. 16 depicts a multivariate correlation of the statistical analysis of the soil data. \|[0046] FIG. 17 depicts a diagram of another exemplary field-scale randomized complete block design used to investigate the synergistic combination of nickel phytomining and enhanced weathering. \|[0047] FIG. 18 depicts the life cycle assessment model for an exemplary 1 kilotonne-scale production. \|[0048] FIGS. 19A and 19B depict the life cycle assessment model for an exemplary 1 megatonne-scale production. \|[0049] FIG. 20 depicts additional data used in the life cycle assessment of an exemplary process. \|DETAILED DESCRIPTION \|[0050] The following description sets forth exemplary compositions, methods, systems, parameters and the like. It should be recognized, however, that such description is not intended as a limitation on the scope of the present disclosure but is instead provided as a description of exemplary embodiments. \|[0051] In one aspect, provided herein is a method of sequestering carbon dioxide comprising providing a weatherable rock comprising one or more metals, subjecting the weatherable rock to conditions sufficient to cause the rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the one or more metals, and wherein the alkalinity facilitates the sequestration of carbon dioxide through the conversion of carbon dioxide to bicarbonate or carbonate, and extracting and processing the released metals to provide a metal-enriched composition. In some embodiments, the conditions cited above comprise growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock. In some embodiments, the conditions comprise growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock and continuously irrigating the one or more metal hyperaccumulator plants using a drip irrigation system. In some embodiments, the extracting and processing the released one or more metals comprises growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock, wherein the one or more metal hyperaccumulator plants accumulate the released one or more metals. In some embodiments the extracting and processing the released one or more metals further comprises processing the metal hyperaccumulator biomass using any suitable technique known in the art to prepare a metal-enriched composition. In some embodiments, the one or more metals comprise a heavy metal. In some embodiments, the one or more metals comprise a toxic metal. In some embodiments, the one or more metals comprise a metal selected from the group consisting of Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the one or more metals comprise cobalt. In some embodiments, the one or more metals comprise chromium. In some embodiments, the one or more metals comprise nickel. In some embodiment the one or more metals comprise any metal that can be hyperaccumulated by a hyperaccumulator plant. In some embodiments, providing the weatherable rock comprises mining the weatherable rock. In some embodiments, providing the weatherable rock further comprises mechanically processing the weatherable rock to reduce the particle size of the weatherable rock to between about 1 pm and about 10 cm. In some embodiments, providing the weatherable rock further comprises admixing the weatherable rock with one or more additional growing media including, for example, soil. \|[0052] In one aspect, provided herein is a method of sequestering carbon dioxide comprising providing a weatherable rock comprising a metal, subjecting the weatherable rock to conditions sufficient to cause the rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide through the conversion of carbon dioxide to bicarbonate or carbonate, and extracting and processing the released metal to provide a metal-enriched composition. In some embodiments, the conditions cited above comprise growing a metal hyperaccumulator plant in a medium comprising the weatherable rock. In some embodiments, the conditions comprise growing a metal hyperaccumulator plant in a medium comprising the weatherable rock and continuously irrigating the metal hyperaccumulator plant using a drip irrigation system. In some embodiments, the extracting and processing the released metal comprises growing a metal hyperaccumulator plant in a medium comprising the weatherable rock, wherein the metal hyperaccumulator plant accumulates the released metal. In some embodiments the extracting and processing the released metal further comprises processing the metal hyperaccumulator biomass using any suitable technique known in the art to prepare a metal-enriched composition. In some embodiments, the metal is a heavy metal. In some embodiments, the metal is a toxic metal. In some embodiments, the metal is selected from the group consisting of Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the metal comprises cobalt. In some embodiments, the metal comprises chromium. In some embodiments, the metal comprises nickel. In some embodiment the metal is any metal that can be hyperaccumulated by a hyperaccumulator plant. \|[0053] In some embodiments, the weatherable rock comprises a magnesium-bearing silicate mineral. In certain embodiments, the magnesium-bearing silicate mineral is in the olivine mineral group. In certain embodiments, the magnesium-bearing silicate mineral is in the serpentinite mineral group. In other variations, any combination of suitable weatherable rocks described herein may be used. \|[0054] In some embodiments, providing the weatherable rock comprises mining the weatherable rock. In some embodiments, providing the weatherable rock further comprises mechanically processing the weatherable rock to reduce the particle size of the weatherable rock to between about 1 pm and about 10 cm. In some embodiments, providing the weatherable rock further comprises admixing the weatherable rock with one or more additional growing media including, for example, soil. \|[0055] In another aspect, provided herein is a method that utilizes plants that are not only tolerant to serpentine, but that evolved especially to live in high alkalinity (e.g., high pH) soils, composed of high percentages of low nutrient and metal heavy soils. These plants that typically take up nickel as a means of protection can be utilized to produce commercial yields of nickel. In certain aspects, provided is a method to bring fresh serpentine-containing rock from nearby quarries, utilizing mechanical activation to grind them to particles, for example micron-sized particles, to increase the reactive surface area, then transported to fields where nickel hyperaccumulating plants have been planted to capture the nickel release from the soil, and also accelerate the release of magnesium ions from the crystal lattice of the serpentine in order to increase the amount of carbon sequestered when those ions run off to the ocean. The methods provided herein overcome the previous blockers that prevented the deployment of terrestrial enhanced weathering for the purposes of carbon removal, and by increasing the revenue streams available to the process are able to make direct and intentional phytomining possible. The methods provided make phytomining a primary mining technique. In some variations, the methods can also use tailings, waste, or overburden from traditional nickel mines. In certain variations, the methods involve actively grinding minerals to below a certain size in order to specifically increase the reactive surface area. Further, in some variations, direct irrigation can be utilized to both enhance the weathering rate, and increase the plant growth, the plant then releases acids that further break down the rocks, releasing magnesium that leads to carbon removal and drawing nickel into the plants, preventing its release into the environment. \|[0056] In some variations of the foregoing, the chemical weathering process results in the formation of new soil minerals. In certain variations of the foregoing, the chemical weathering process results in fully weathered rock. In some embodiments, the weathering process results in fully weathered rock within about 20 years; or between 1 year and 20 years; or within about 1 year, about 2 years, about 3 years, about 4 years, about 5 years, about 6 years, about 7 years, about 8 years, about 9 years, about 10 years, about 11 years, about 12 years, about 13 years, about 14 years, about 15 years, about 16 years, about 17 years, about 18 years, about 19 years, or about 20 years. \|[0057] With reference to FIG. 1, depicted is an exemplary process 100 for obtaining metal using weatherable rock and phytomining. Step 102 involves mechanically grinding a weatherable rock to provide a particulate weatherable rock composition. In step 104, the particulate weatherable rock composition is combined with a soil to provide a weatherable rock-enriched soil. In step 106, a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil is grown. Then, in step 108, the metal hyperaccumulator plant is harvested. In step 110, the harvested metal hyperaccumulator plant is processed using any suitable techniques or methods known in the art to provide a substantially pure metal. In some variations of the process, step 110 may be optional. For example, in certain variations, the process described herein does not require harvesting of the metal from the plant to obtain a substantially pure metal. In other variations, the process further includes harvesting of the metal from the plant to obtain a substantially pure metal.\|[0058] Thus, in some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising magnesium, and a metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil; harvesting the metal hyperaccumulator plant; and processing the harvested metal hyperaccumulator plant to provide a substantially pure metal. In some embodiments, processing the harvested metal hyperaccumulator plant comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide a substantially pure metal by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide a substantially pure metal may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 20% by weight of magnesium and 0.1% by weight of the metal. In some embodiments, the metal-enriched ash comprises at least 5% of the metal by weight. \|[0059] In some embodiments, provided is a method for preparing one or more metals comprising mechanically grinding a weatherable rock comprising magnesium, and one or more metals to provide a particulate weatherable rock composition; either combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil or using the particulate weatherable rock composition directly as a weatherable rock- enriched soil without combining it with any additional media; growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil, wherein each of the one or more plants is a hyperaccumulator of at least one of the one or more metals; harvesting the one or more metal hyperaccumulator plants; and processing the one or more harvested metal hyperaccumulator plants to provide one or more substantially pure metals. In some embodiments, processing the one or more harvested metal hyperaccumulator plants comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide one or more substantially pure metals by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide one or more substantially pure metals may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 20% by weight of magnesium and 0.1% by weight of each of the one or more metals. In some embodiments, the metal-enriched ash comprises at least 5% of each of the one or more metals by weight.\|[0060] In some embodiments, provided is a method for obtaining one or more substantially pure metals comprising mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium and at least 0.1% by weight of each of the one or more metals to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil, wherein each of the one or more plants is a hyperaccumulator of at least one of the one or more metals; harvesting the one or more metal hyperaccumulator plants; and processing the one or more harvested metal hyperaccumulator plants to provide one or more substantially pure metals. \|[0061] In some variations, substantially pure metal refers to a metal that is at least 90%, at least 95%, at least 96%, at least 97%, at least 98%, at least 99%, at least 99.9%, at least 99.99%. at least 99.999%, or at least 99.9999% pure by weight. \|[0062] In some embodiments, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the metal hyperaccumulator plant is growing. In some embodiments, about 10% of the Mg by weight is weathered per year. In some embodiments, about 90% of the Mg by weight is weathered per month. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated over a period of about 20 years. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated over a period of less than about 20 years. In any of the foregoing embodiments, the weight of Mg2+ refers to the weight of the magnesium component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts that the Mg2+ is a part of. \|[0063] In some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising calcium and a metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil; harvesting the metal hyperaccumulator plant; and processing the harvested metal hyperaccumulator plant to provide a substantially pure metal. In some embodiments, processing the harvested metal hyperaccumulator plant comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide a substantially pure metal by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide a substantially pure metal may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 10% by weight of calcium and at least 0.1% by weight of the metal. In some embodiments, the metal-enriched ash comprises at least 5% of the metal by weight. \|[0064] In some embodiments, Ca2+ is leached at a rate of at least 1% by weight of the total Ca2+ in the weatherable rock per year from the weatherable rock-enriched soil while the metal hyperaccumulator plant is growing. In some embodiments, about 10% of the Ca by weight is weathered per year. In some embodiments, about 90% of the Ca by weight is weathered per month. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated over a period of about 20 years. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated over a period of less than about 20 years. In any of the foregoing embodiments, the weight of Ca2+ refers to the weight of the calcium component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts that the Ca2+ is a part of. \|[0065] In some embodiments, the rate at which Mg2+ is leached is measured by measuring the concentration of the Mg2+ in the water used to irrigate the hyperaccumulator plant. In some embodiments, the rate at which Ca2+ is leached is measured by measuring the concentration of Ca2+ in the water used to irrigate the hyperaccumulator plant. \|[0066] In some variations of the foregoing, the weatherable rock comprises between 0.01% and 20% of the metal by weight. In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of the metal by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of the metal. \|[0067] In some embodiments, the metal comprises Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the metal comprises a rare earth metal. In some embodiments, the metal comprises nickel. In some embodiments, the metal comprises cobalt. In some embodiments, the metal comprises chromium. In some embodiments, the metal is a metal that can be hyperaccumulated by a hyperaccumulator plant. In some embodiments, the metal is a metal found in a weatherable rock. In some embodiments, the metal is a metal found in a weatherable rock that can be hyperaccumulated by a hyperaccumulator plant. \|[0068] In some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising magnesium and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; liberating nickel from the weatherable rock by subjecting the weatherable rock-enriched soil to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein acid is not added to the weatherable rock- enriched soil; growing a plant that is a hyperaccumulator of nickel in the weatherable rock- enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide substantially pure nickel. \|[0069] In some embodiments, the amount of carbon dioxide emitted from the weathering of the weatherable rock is less than amount of carbon dioxide sequestered from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide emitted from the weathering of the weatherable rock, harvesting the nickel hyperaccumulator plant, and processing the harvested nickel hyperaccumulator plant is less than amount of carbon dioxide sequestered from the weathering of the weatherable rock. \|[0070] In some embodiments, provided is a method for preparing nickel metal comprising mechanically grinding a weatherable rock comprising magnesium, and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel. In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash and refining the nickel-enriched composition to provide a substantially pure nickel by weight. In some embodiments, processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 10% by weight of magnesium and at least 0.1% by weight of nickel. In some embodiments, the nickel-enriched ash comprises at least 5% nickel by weight. \|[0071] In some variations of the foregoing, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the nickel hyperaccumulator plant is growing. \|[0072] In some variations of the foregoing, the weatherable rock comprises between 5% and 60% Mg by weight. In some embodiments, the weatherable rock comprises between 25% and 50% Mg by weight. In some embodiments, the weatherable rock comprises about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, or about 70% Mg by weight. \|[0073] In some variations of the foregoing, the weatherable rock comprises between 5% and 60% Ca by weight. In some embodiments, the weatherable rock comprises between 25% and 50% Ca by weight. In some embodiments, the weatherable rock comprises about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, or about 70% Ca by weight. \|[0074] In some variations of the foregoing, the weatherable rock comprises between 0.01% and 20% of nickel by weight. In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of nickel by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of nickel. \|[0075] In some variations of the foregoing, the weatherable rock comprises nickel and Mg. In some embodiments, the weatherable rock comprises between 0.01% and 25% of nickel by weight and between 5% and 60% of Mg by weight. In some embodiments, the weatherable rock comprises between 0.01% and 25% of nickel by weight and between 25% and 50% of Mg by weight. \|[0076] In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of nickel by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of nickel. \|[0077] In some variations of the foregoing, the nickel-enriched ash composition comprises between 1% and 99.8% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 1% and 35% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 1% and 30% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 30% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 20% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 15% nickel by weight. In some embodiments, the nickel- enriched ash composition comprises about 0.1%, about 0.5%, about 1%, about 1.5%, about 2%, about 2.5%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, or about 40% nickel by weight. \|[0078] In some variations of the foregoing, refining the nickel-enriched composition provides a nickel that is at least 15%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 98%, at least 99%, at least 99.9%, at least 99.9%, at least 99.99%, at least 99.999%, or at least 99.9999% pure by weight. In some embodiments, refining the nickel-enriched composition provides a nickel that is between 15% and 100% pure by weight. \|[0079] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprises drying the nickel hyperaccumulator plant to provide a dried biomass composition, crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a nickel-enriched ash composition. In some embodiments, the ashing is performed at a temperature of about 500 °C. \|[0080] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises directly leaching the harvested nickel hyperaccumulator plant to provide a leachate; purifying the leachate to provide a Ni-enriched leachate; and further processing the Ni-enhanced leachate to provide a substantially pure nickel. In some embodiments, the direct leaching is performed using a hydrothermal process. In some embodiments, the direct leaching is performed in acid. In some embodiments, the acid is sulfuric acid. In some embodiments, the acid is hydrochloric acid. In some embodiments purifying the leachate comprises purifying the leachate using column chromatography. In some embodiments purifying the leachate comprises purifying the leachate using solvent extraction. In some embodiments purifying the leachate comprises purifying the leachate using ion exchange chromatography. In some embodiments, further processing the Ni-enhanced leachate comprises electrowinning the nickel. \|[0081] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash, leaching the nickel-enriched ash composition to provide a leachate, treating the leachate to provide ammonium Ni sulfate hexahydrate (ANSH), and processing the ANSH to obtain a substantially pure nickel. In some embodiments, the leaching is performed in acid. In some embodiments treating the leachate comprises neutralizing the leachate using a base to provide a first treated leachate, adding a fluoride source to the first treated leachate to provide a second treated leachate, adding ammonium sulfate to the second treated leachate to provide a third treated leachate, and drying the third treated leachate to provide ANSH. In some embodiments, the base is Ca(OH)2. In some embodiments, the fluoride source is NaF. In some embodiments, treating the leachate comprises purifying the ANSH via recrystallization. \|[0082] In some embodiments, provided is a method for preparing nickel catalysts comprising mechanically grinding a weatherable rock comprising magnesium, and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide nickel catalysts. In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash, leaching the nickel-enriched ash to provide a leachate, and further processing the leachate to provide nickel catalysts. In some embodiments, the ashing is performed at a temperature of 500 °C. In some embodiments, the leaching is performed in acid. In some embodiments, the acid is hydrochloric acid. In some embodiments, further processing the leachate to provide nickel catalysts comprises dispersing the leachate onto montromorillonite K10. In some embodiments, the weatherable rock comprises at least 10% by weight of magnesium and at least 0.1% by weight of nickel.\|[0083] In some embodiments, the amount of carbon dioxide sequestered is on the tonne scale for every tonne of nickel metal that is produced. In some embodiments, at least 1 tonne, at least 5 tonnes, at least 10 tonnes, at least 20 tonnes, at least 30 tonnes, or at least 40 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. In some embodiments, between 1 tonne and 100 tonnes, or between 10 tonnes and 100 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. In some embodiments, between 100 tonnes and 500 tonnes, or between 300 tonnes and 500 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. \|[0084] In some embodiments, the weatherable rock comprises an ultramafic rock. In some embodiments, the weatherable rock comprises serpentine. In some embodiments, the weatherable rock comprises serpentinite. In some embodiments, the weatherable rock comprises olivine. In some embodiments, the weatherable rock contains less than 1% by weight of nickel. In some embodiments, the weatherable rock contains a metal that can be hyperaccumulated by a hyperaccumulator plant. \|[0085] In some embodiments, the method further comprises mining the weatherable rock. In other embodiments, the method further comprises transporting the mined weatherable rock from a mining location to a grinding location. \|[0086] In some embodiments, mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock. In some embodiments, the energy used to mechanically grind the rock comes from renewable sources. \|[0087] In some embodiments, the particulate weatherable rock composition has an average particle size between about 1 pm and about 10 mm, between about 1 pm and about 10 cm, between about 1 pm and about 20 cm, between about 1 pm to about 5 mm, between about 1 pm to about 3 mm, or between about 100 pm to about 3 mm. \|[0088] In some embodiments, the weatherable rock-enriched soil comprises between 10% and 100%, between 70% and 100%, between 70% and 90%, between 70% and 80%, or between 80% and 90% particulate weatherable rock composition by weight. In certain embodiments, the weatherable rock-enriched soil comprises about 30%, about 40%, about 50%, about 60%, about 70%, about 80%, about 90%, or about 100% particulate weatherable rock composition by weight.\|[0089] In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of silicate rocks. In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of serpentinite rocks. In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of olivine rocks. In some embodiments, natural weathering of serpentinite rocks results in weatherable rock-enriched soil with high nickel concentrations. \|[0090] In some embodiments, the nickel hyperaccumulator plant is a plant belonging to the genus Odontarrhena. In some embodiments the plant belongs to the genus Alyssum. In some embodiments the plant belongs to the family Brassicacaea. In some embodiments the plant belongs to the genus Bornmuellera. In some embodiments the plant belongs to the genus Thlaspi. In some embodiments, the plant is Alyssum Murale. In some embodiments, the plant is of the genus Odontarrhena. In some embodiments, the plant is Odontarrhena chalcidica. In some embodiments, the plant is Odontarrhena decipiens. In some embodiments, the plant is Berkheya coddii. In some embodiments, the plant is B. emarginata. In some embodiments, the plant is Stackhousia tryonii. In some embodiments, the plant is Phyllanthus balgooyi. In some embodiments, the plant is Rinorea bengalensis. In some embodiments, the plant may be a tree, bush, or vine. In some embodiments, the plant is a genetically modified plant. In some embodiments, the plant is any plant capable of hyperaccumulating a metal found in a weatherable rock. In some embodiments, the plant is any plant capable of hyperaccumulating nickel. In some embodiments, the plant is any hyperaccumulator plant species of the class known as a hypernickelophores, containing more than 1,000 pg Ni g 1. \|[0091] In some embodiments, the nickel hyperaccumulator plant is grown inside of a greenhouse. In some embodiments, the nickel hyperaccumulator plant is grown inside of a vertical farm. In some embodiments, the nickel hyperaccumulator plant is grown hydroponically. In some embodiments, the nickel hyperaccumulator plant is grown under a polyethylene film (e.g., a polytunnel). \|[0092] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the weathering rate of the weatherable rock. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the efficiency of nickel uptake by the plant. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the weathering rate of the weatherable rock and the efficiency of nickel uptake by the plant. \|[0093] In some embodiments, the environmental conditions of the weatherable rock- enriched soil are controlled to cause the weatherable rock to undergo a chemical weather process at an accelerated rate relative to natural chemical weathering environmental conditions. In some embodiments, the conditions cited above comprise growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil. In some embodiments, the conditions comprise growing one or more metal hyperaccumulator plants in a weatherable rock-enriched soil and continuously irrigating the one or more metal hyperaccumulator plants using a drip irrigation system. In some embodiments, the temperature, pH, irrigation, or bioactivity of the weatherable rock-enriched is controlled. \|[0094] In some embodiments, the rate of weathering of the weatherable rock is between about 0% and about 40% by mass of the weatherable rock between about 12 months and about 72 months from the date of combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil and planting the hyperaccumulator plant in the weatherable rock-enriched soil. Any suitable methods known in the art may be used to determine the rate of weathering of the weatherable rock. For example, in one variation, the foregoing rates of weathering may be calculated using the Arrhenius equation. \|[0095] In some embodiments, the weathering rate is calculated by measuring the accumulation of rock-derived cations (e.g., Ca, Mg, Na, and K) in plant, soil, and/or aqueous effluent associated within a certain plot of land and subtracting the baseline amount of the corresponding cation measured in a corresponding control plot. For example, the net accumulation of Ca-cations due to mineral dissolution of weatherable rock can be calculated by subtracting the amount of Ca-cations measured in a control plot from the total amount of Ca-cations calculated by totaling the amount of Ca-cations in the water and/or effluent, the Ca-cations in plant tissues, and Ca-cations in the soil cation exchange pool. The amount of Ca-cations attributable to the weathering of weatherable rock can then be converted into spatially-averaged cation weathering rates (per unit of land area) or rates related to mineral surface area. In some embodiments, the weatherable rock is calculated in the number of moles of calcium, magnesium, sodium, and/or potassium released from the weatherable rock material into the soil per hectare of treated land per annum.\|[0096] In some embodiments, the weathering rate of the weatherable rock increases when the average particle size of the weatherable rock decreases. \|[0097] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to increase the weathering rate of the weatherable rock. In some embodiments, the environmental parameter that is optimized to increase the weathering rate of the weatherable rock is temperature. In some embodiments, the temperature of the surrounding air (e.g., climate) is increased to increase the weathering rate of the weatherable rock. In some embodiments, the temperature of the topsoil (e.g., where the weatherable rock is admixed into the soil) is increased to increase the weathering rate of the weatherable rock. In some embodiments, the amount of irrigation of the soil admixed with the weatherable rock is increased to increase the weathering rate of the weatherable rock. In some embodiments, the pH of the soil admixed with the weatherable rock is increased to decrease the weathering rate of the weatherable rock. In some embodiments, the pH of the soil admixed with the weatherable rock is decreased to increase the weathering rate of the weatherable rock. \|[0098] In some embodiments, the weathering rate of the weatherable rock is increased by increasing the amount of biological activity of the soil admixed with the weatherable rock. In certain embodiments, the increased biological activity of the soil is measured by the amount of carbon dioxide produced by the microbes per a given amount of the soil. In certain embodiments, the increased biological activity of the soil is measured by the amount of nitrogen-cycling and secretion of organic acids by plant roots and mycorrhizal fungi present in the soil. \|[0099] In some embodiments, increasing the concentration of Mg2+ ions in the soil admixed with the weatherable rock increases the weathering rate of the weatherable rock. In some embodiments, increasing the concentration of Ca2+ ions in the soil admixed with the weatherable rock increases the weathering rate of the weatherable rock. In certain variations, higher soil Ca and Mg content may decrease the weathering rate of rock material added to the soil, because chemical conditions in the groundwater may approach saturation for certain Ca- (and Mg-) bearing minerals. \|[0100] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the accumulation of nickel by the plant. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the growth rate of the plant. In some embodiments, the humidity, temperature, or lighting of the environment in which the nickel hyperaccumulator plant is grown are controlled. In some embodiments, the nickel hyperaccumulator plant is grown in an outdoor field. \|[0101] In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to maximize the accumulation of nickel by the hyperaccumulator plant. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is between about 5 tonnes and 300 tonnes. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is between about 10 tonnes and 50 tonnes. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is about 37 tonnes. \|[0102] In some embodiments, the amount of nickel accumulated by a nickel hyperaccumulator plant increases proportionally with the amount of weatherable rock mixed into the soil in which the plant is grown. In some embodiments, increasing the amount of weatherable rock mixed in the soil does not result in an increase in the amount of nickel accumulated by a hyperaccumulator plant growing in the soil. In certain embodiments, high amounts of weatherable rock mixed into the soil result in high alkaline (e.g., high pH) soils which can negatively impact the mobility of the one or more metals released from the weatherable rock during the weathering process. \|[0103] In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown and the environmental conditions under which the hyperaccumulator plant is grown are optimized to control the pH of the soil. In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to control the pH of the soil. In some embodiments, an increase in the pH of the soil decreases the mobility of the one or metals released by the weatherable rock mixed in the soil. In some embodiments, decreased mobility of the one or more metals in the soil results in lower accumulation of the metals by a hyperaccumulator plant of the same metal growing in the soil. In some embodiments, an increase of the pH of the soil decreases the amount of metal accumulated by the hyperaccumulator plant growing in the soil, the mobility of the one or metals released by the weatherable rock, or both. \|[0104] In some embodiments the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to maximize the growth rate of the hyperaccumulator plant. \|[0105] In some embodiments, at least 5 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, at least 10 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 10 tonnes and 100 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 5 tonnes and 10 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 25 tonnes and 50 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 35 tonnes and 40 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 100 tonnes and 200 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, about 150 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 400 tonnes and 800 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. . In some embodiments, about 600 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. \|[0106] In some embodiments, at least about 20 tonnes of nickel hyperaccumulator biomass is grown per hectare. In some embodiments, at least about 400 kg, at least about 500 kg of nickel, at least about 600 kg, at least about 700 kg, at least about 800 kg, at least about 900 kg, or at least about 1,000 kg of nickel is produced per hectare. In other variations, between about 100 kg and 5000 kg, or between 250 kg and 1000 kg, or between 400 kg and 1000 kg of nickel is produced per hectare.\|[0107] In some embodiments, between about 5 tonnes and about 50 tonnes, between about 100 tonnes and about 700 tonnes, between about 500 tonnes and about 700 tonnes, between about 100 tonnes and about 600 tonnes, between about 200 tonnes and about 600 tonnes, between about 300 tonnes and about 600 tonnes, between about 400 tonnes and about 600 tonnes, between about 500 tonnes and about 600 tonnes, between about 100 tonnes and about 500 tonnes, between about 200 tonnes and about 500 tonnes, between about 300 tonnes and about 500 tonnes, between about 400 tonnes and about 500 tonnes, between about 100 tonnes and about 400 tonnes, between about 200 tonnes and about 400 tonnes, between about 300 tonnes and about 400 tonnes, between about 100 tonnes and about 300 tonnes, between about 200 tonnes and about 300 tonnes, or between about 100 tonnes and about 200 tonnes of weatherable rock are mixed into the soil for every hectare on which the hyperaccumulator plant is grown. In some embodiments, about 500 tonnes about 600 tonnes, or about 700 tonnes of weatherable rock are mixed into the soil for every hectare on which the hyperaccumulator plant is grown. \|[0108] In some embodiments, the amount of carbon dioxide sequestered is proportional to the number of Mg2+ ions liberated from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide sequestered per hectare is proportional to the number of Mg2+ ions liberated from the weathering of the weatherable rock mixed into the soil for every hectare. \|[0109] In some embodiments, the amount of carbon dioxide sequestered is proportional to the number of Ca2+ ions liberated from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide sequestered per hectare is proportional to the number of Ca2+ ions liberated from the weathering of the weatherable rock mixed into the soil for every hectare. \|[0110] In some embodiments, the nickel hyperaccumulator plant is harvested mechanically. In some embodiments, the nickel hyperaccumulator plant is harvested manually. In some embodiments, the nickel hyperaccumulator plant is harvested by an automated process. \|[0111] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil. In some embodiments, the plant is irrigated using a drip irrigation system. In some embodiments, the plant is irrigated using sprinkler systems. In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises intermittently irrigating the weatherable rock-enriched soil. In some embodiments, the plant is irrigated using a flood irrigation approach. In some embodiments, the plant is irrigated using traditional irrigation. \|[0112] In some embodiments, the pH of the weatherable rock-enriched soil is above 7. In some embodiments, the pH of the weatherable rock-enriched soil is between 7 and 14. In some embodiments, the pH of the weatherable rock-enriched soil is between 5 and 14. In some embodiments, increasing the content of the weatherable rock of the weatherable rock- enriched soil increases the pH of the soil. \|[0113] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprise drying the nickel hyperaccumulator plant to provide a dried biomass composition; crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a nickel-enriched composition. \|[0114] In some embodiments, the method further comprises quantifying the amount of carbon dioxide that is released or sequestered in one or more steps of any of the methods described herein. In some embodiments, the amount of carbon dioxide released or sequestered by a process is measured directly. In some embodiments, the amount of carbon dioxide released or sequestered by a process is measured using a proxy. In some embodiments, the quantity of Mg2+ is used as a proxy to quantify the amount of carbon dioxide sequestered by chemical weathering of the weatherable rock. \|[0115] In another aspect, provided herein is nickel metal prepared according to any of the methods described above. \|[0116] In another aspect, provided herein is a processed nickel composition comprising a substantially pure nickel, and one or more of the following: Nickel rich ashes also containing K, Ca, oxides (e.g., NiO, MgO), carbonates (e.g., K2CO3, CaCO3, K2Ca(CO3)2), K2SO4, precipitated gypsum, low-mass carboxylic acids, Ni-bearing organic and inorganic compounds. Ni-based compounds such as NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, Ni oxalate, and Ni sulfate. In some variations of the foregoing, the processed nickel composition is at least 15%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 98%, at least 99%, at least 99.8%, at least 99.9%, at least 99.99%, at least 99.999%, or at least 99.9999% pure by weight. In some embodiments, the processed nickel composition is between 15% and 100% pure by weight. \|[0117] In another aspect, provided herein is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: Nickel rich ashes also containing K, Ca, oxides (e.g., NiO, MgO) and carbonates (e.g., K2CO3, CaCCh, KiCa CCh ), K2SO4, precipitated gypsum, low-mass carboxylic acids, Ni-bearing organic and inorganic compounds. Ni-based compounds such as NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, Ni oxalate, and Ni sulfate. In some embodiments, provided herein is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: Ca, Fe, K, Mg, carbonates (e.g., K2CO3, CaCOs, or K2Ca(CO3 ), P, plant cells, C, H, N, O, hydroxyapatite, oxy -hydroxyapatite, or oxides (e.g., NiO, CaO, MgO, or MgNiO2). In some embodiments, the nickel-enriched ash comprises between 5% and 100% nickel by weight. \|[0118] In any of the foregoing embodiments, the weight of nickel refers to the weight of the nickel component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts, respectively, that the nickel is a part of. \|EXAMPLES \|[0119] The presently disclosed subject matter will be better understood by reference to the following Examples, which are provided as exemplary of the invention, and not by way of limitation. \|Example 1: Assessment of weathering rates for different soil and plant configurations\|[0120] Samples of O. decipiens (a close relative to the hyperaccumulator known in the art as O. chalcidica or A. morale) were shipped to a testing facility. There, the seeds were separated from the remainder of the plant biomass, soaked in water to prepare them for germination, and germinated. The germinated seeds were observed to have root systems. Separately, a sample of serpentinite rock was obtained, and was ground into a fine powder, herein referred to as “serpentine soil”. \|[0121] Nine sample planters were prepared, with each planter containing a specific ratio of serpentine soil to potting soil (including both pure potting soil and pure serpentine soil). Seeds of the hyperaccumulator plants were planted in eight of the nine planters, and one planter was left with no seeds, as a control. Additionally, NPK hydroponic fertilizer was added in different concentrations to the continuous, closed-loop irrigation systems of two of the planters. The experimental conditions for each planter are illustrated in FIG. 2. \|[0122] Because Mg2+ is released in the weathering reaction of serpentine, the quantity of Mg2+ leached from the soils in each planter was used as a proxy for the rate of weathering that occurred under each condition. Over the course of 4 months, the total concentration of Mg2+ leached into the closed-loop irrigation system was measured for each of the nine planter conditions shown in FIG. 2. The results of these measurements are shown in FIG. 3. Surprisingly, it was found that quantity of Mg2+ leached by the soil mixtures increased over time as the plants grew. Further, the rate of weathering, as assessed using Mg2+ leaching as a proxy, was found to correlate to plant biomass growth. \|Example 2: Field-scale enhanced rock weathering experiment \|[0123] A field-scale trial was employed to investigate the synergistic combination of nickel phytomining and enhanced weathering. The principal aim of this experiment was to evaluate the scope for nickel extraction by the hyperaccumulator plant Odontarrhena decipiens and to quantify the carbon capture potential of crushed serpentinite rock added to the naturally occurring serpentine agricultural soil. \|[0124] A 112 m x 168 m field site was selected for this trial based on aerial photography and ground observations. Four permanent reference points for determining precise locations were established by cementing steel posts into the ground at the comers of the field site. The area was then partitioned into four equally-sized rectangular blocks, each measuring 56 m x 84 m. A scale diagram of the randomized complete block design used in the trial is shown in FIG. 4. These blocks represent replicates, such that each block contained eight randomized 12 m x 18 m plots (one for each of the eight rock treatments) separated by an 8 m margin of untreated land. The amount of rock treatment added to each plot as measured in tonnes of serpentinite rock per hectare is shown in FIG. 4. The randomized complete block design accounts for the effects of extraneous variables (e.g. hydrological gradients across the site) and hence, mitigates bias caused by inherent variation. \|[0125] The entire field site was tilled prior to the trial. Crushed serpentinite rock was sourced from a nearby quarry and applied by hand to the soil surface of each plot at rates ranging from 9.375 to 600 tonnes per hectare, whereby the next higher rate was set to be double the previous as illustrated in FIG. 4. Each block also contains a ‘control’ treatment where no serpentinite rock is added (i.e. 0 tonnes per hectare), against which all other treatments were compared statistically. The applied rock material was incorporated into the soil to an approximate depth of 150 mm using a rotavator. One-year-old Odontarrhena decipiens specimens were then transplanted into each plot, in thirteen rows with 1 m rowspacing and 0.5 m spacing between the individual plants. Organic fertilizers, pesticides, and fungicides were added to the experimental plots to ensure baseline crop performance and mitigate pest/pathogen interference in all treatments. \|[0126] At the beginning of the experiment, over a hundred mesh bags were filled with 0.4 g of crushed serpentinite and buried in the plots at soil depths between 50-200 mm. Retrieval of the grains from these bags at the end of the trial permits the direct assessment of mineral weathering through X-ray analysis. \|Soil sample collection and measurements \|[0127] Before applying the serpentinite rock material, fifteen baseline soil samples were collected from each block using a steel auger and following a W-shaped sampling pattern. These initial (pre-planting, pre-rock application) soil samples are taken from three depths: 0- 0.3 m, 0.3-0.6 m, and 0.6-0.9 m. Soils are then passed through a 2 mm mesh size sieve, air dried, and tested for the following physical and chemical parameters: pH (in H2O and IM KC1); organic matter and humus %; plant-available nitrogen, phosphorus and potassium; soil texture (sand/silt/clay %); cation exchange capacity; and, total and plant-available Ca, Mg, K, Na, Fe, Cd, Co, Cr, Cu, Mn, Ni, Pb, and Zn. Further soil samples were collected monthly from each of the thirty-two experimental plots and tested for pH, electrical conductivity, cation exchange capacity, and plant-available cations. These data were used to monitor changes in the concentrations of plant-available nutrients and nickel over time, and to estimate rock weathering and carbon dioxide capture rates via a conventional mass balance approach, in combination with novel quantification methods. \|Plant sample collection and measurements \|[0128] Aboveground plant tissues are harvested from all plots after a suitable time (e.g., approximately 6-8 months) after the trial began. Plant materials are dried and weighed to determine crop yields, and ground for analysis of nutrients and metals. These data are used to measure the efficiency of nickel uptake by the hyperaccumulator plants, and to evaluate the correlation between rock application and nickel uptake rates. Moreover, values for total uptake of calcium, magnesium, potassium and sodium are fed into mass budget calculations for carbon capture quantification. \|[0129] Aboveground plant tissues were harvested from five different mature hyperaccumulator plant specimens randomly selected from all plots after a suitable time (e.g., approximately 6-8 months) after the trial began. Plant samples were washed with distilled water, dried in a forced-air oven at 60 °C for 48 hours, and powdered separately using a laboratory grinding mill. These plant samples were used to determine total heavy metal concentrations in the plant tissues. \|Soil pH and electrical conductivity measurements \|[0130] The pH and the electrical conductivity (EC) of the soil samples determined using a Combined Conductivity /pH Meter equipped with a temperature input, which internally corrects for the effect of temperature on measured values. pH and EC were standardized using a 3-point calibration protocol with certified reference solutions (buffers at pH 4.00, 7.00, and 14.00; EC standards at 12.88 mS, 1413 pS, and 84 pS). To streamline the measurements, pH and EC were tested sequentially from the same sample. For each soil sample, 15.0000 ± 0.0005 g of soil was weighed into a 50 mL polypropylene centrifuge tube and combined with 30.0000 ± 0.0150 mL of ultrapure water (resistivity of 18.2 MQ-cm at 25 °C). The tubes were stoppered, agitated on a rotary shaker for 3 minutes, unstoppered and then left to equilibrate with the atmosphere for 30 minutes. An additional three replicates of control soil (initial/baseline soil containing no additives) were prepared and used to precondition the pH and conductivity electrodes prior to analysis of the experimental samples. This preconditioning process shortens the timescales for stable measurements and mitigates measurement error in the first few experimental samples (e.g. due to contamination with trace amounts of buffer solution). To obtain pH measurements, the pH electrode was swirled into the soil-water mixture’s supernatant for 10 seconds, and then gently released into the slurry until the instrument identified that a stable pH reading was achieved (or 3 minutes after initial insertion, where stabilization was not achieved). pH measurements were recorded to 0.001 pH units, and the electrode was rinsed thoroughly with ultrapure water between samples. To obtain EC measurements, the conductivity electrode was inserted into the soilwater mixture’s supernatant and held until the instrument indicated that a stable EC reading was achieved (or 1 minute after initial insertion, where stabilization was not achieved). EC measurements were recorded to four significant figures, and the electrode was rinsed thoroughly with ultrapure water between samples. \|Soil analysis methods for total heavy metals \|[0131] The soil samples were tested for total heavy metals by first drying a test portion of the soil and reducing the grain size of the soil to below a particle size of 250 microns. Each test portion of the soil was then weighed (0.5 g to 1.0 g based on dry mass) and transferred to a microwave extraction vessel. A few drops of water were then added to the extraction vessel before adding a HC1 and nitric acid solution and mixing well. The temperature of the extraction mixture was increased at a rate of approximately 10 °C/min to 175 ± 5 °C using a microwave digestion system. The amount of total Ni in the soil samples was then determined using ICP-OES. \|Availability ofNi with Mehlich-1 digestion \|[0132] The soil samples were prepared by mixing 5 g of the soil samples with 20 mL of a Mehlich-1 extraction solution consisting of a mixture of HC1 and H2SO4. The mixture was then stirred for 5 min at 180 cycles/min after which the suspension was allowed to rest for 16 h before decanting off the supernatant The total amount of Ni in the soil samples was then determined by testing an aliquot of the supernatant using ICP-OES. \|Other analytical methods \|[0133] It should be understood that one or more additional techniques may be used to determine the amount of Ni in the soil, the amount of rock-derivable cations in the tissue of the hyperaccumulator plants or the soil, the amount of heavy metals in the tissue of the hyperaccumulator plants or the soi, the pH of the soil, the electrical conductivity of the soil, and other aspects of the weatherable rock, soil, and hyperaccumulator plants, including quantification of the weathering rate. For example, X-ray fluorescence analysis of weathered rock material (retrieved from mesh bags buried in the plots) is used to quantify changes in grain surface chemistry. These data provide an independent method for mineral weathering rate quantification. The loss of cations from the added rocks may serve as a proxy for the accumulation of cations released from this process in the plant and soil. \|Determination of total heavy metal and Ca, Mg, K concentrations in plants with digestion\|[0134] Aboveground plant tissues were digested in an acid solution (HNO3 65% and H2O2 30%) using a microwave digestion system to determine total heavy metal concentrations in plants. A sample of the plant matter (300 mg) was mixed with 2 mL of HNO3 and 2 mL of H2O2, stirred for at least 20 min, and then digested using a microwave digestion system. Plant tissue samples calibration curves were plotted from Ni concentrations of 2, 4 and 6 mg/L. The solution was diluted 20 times. The amount of Ni in the plant tissue samples was then determined using ICP-OES. \|Results and Analysis \|[0135] Approximately 8 months after the trial began, representative soil samples were collected from the plots for analysis. As shown in FIG. 5, increasing serpentinite application rates resulted in increasing soil pH. Moreover, application rates above 0.9375 kg m 2 resulted in statistically significant increases in soil pH with respect to the control soils, where no serpentinite rocks were added, which is evidence of chemical weathering of the added serpentinite rock. Surprisingly, soil pH continued to increase with increasing application rates, and rose substantially to the highest recorded level at the highest application rate (60 kg m 2) as shown in FIG. 5. Chemical weathering of the added alkaline minerals (e.g. serpentinite rock) will lead to carbon dioxide sequestration. Enhanced weathering of the added rock material is also supported by evidence of elevated soil electrical conductivity (EC) following rock applications as shown in FIG. 6. Higher EC indicates the release of cations due to rock dissolution, and similarly represents evidence for chemical weathering of the serpentinite rock applied to the soil. This chemical weathering leads to carbon dioxide sequestration. \|[0136] Amendment of soils with serpentinite rock also resulted in higher nickel uptake into the tissues of the hyperaccumulator plants as compared to the hyperaccumulator plants grown in the control soils, with the highest nickel yields observed in soils amended with 3.75 to 15 kg m 2 of serpentinite rock as shown in FIG. 7. The mean total Ni yield from the hyperaccumulator plants was calculated by multiplying the (dry) biomass yield by the (dry) biomass Ni concentration. Mean total Ni yields from the hyperaccumulator plants ranged from around 1.4 g Ni m 2 (14 kg Ni ha 1) in the control plots to a peak of about 2.5 g Ni m 2 (25 kg Ni ha 1) in the plots treated with 15 kg m 2 (150 t ha 1) of serpentinite rock. Plants grown on soils with elevated pH will typically accumulate less nickel. Surprisingly, nickel yields increased in the soils amended with 3.75 to 15 kg m 2 of serpentinite rock, which implies that the combination of enhanced weathering of serpentinite and nickel hyperaccumulators realized a synergistic benefit. Overall, this data indicates mass transfer of Ni from the applied serpentinite rock into the tissues of the hyperaccumulator plants. \|[0137] Timeseries data for soil-extractable Ni was determined by a Mehlich 1 extraction procedure and confirms that soil concentrations increased in all plots treated with serpentinite rock between when the trial began (0 m) and the following spring (~5 m), when the hyperaccumulators would have exhibited low primary production as shown in FIG. 8. However, the subsequent steep reduction in soil Ni concentrations between spring (~ 5 m) and mid-summer (~7 m) is evidence for the uptake of soil Ni and depletion of the soil Ni pool by the hyperaccumulator plants at a time of increasing primary productivity as shown in FIG. 8. This data is evidence of the synergy between the two processes because depletion of the soil nickel pool by hyperaccumulator plants can be offset through the weathering of additional nickel bearing-minerals (e.g., serpentinite) introduced to the soil, resulting in carbon negative nickel recovery. \|Statistical analyses \|[0138] Statistical analysis was also performed to determine the significance of the relationships between rock application, plant nickel uptake, and (potential) carbon capture rates. Statistical analysis of the soil data was performed using a linear mixed model with fixed model Treatment * Time and random model of Block/Plot. Where appropriate, variables were first transformed to ensure homogeneity of variance. F statistics were obtained using the Kenward-Roger approximation. Statistical analysis of the plant data was performed using a linear model accounting for differences between blocks. A third order polynomial was fitted over application rate with highest order terms successively dropped if found to be non- significant. \|[0139] Regarding soil pH, statistically significant differences were observed both between treatments (F4, 12=21.54, p < 0.0001) and over time (F3, 45=7.18, p=0.0005). Predicted means and standard errors for each significant main effect is shown in FIGS. 9 and 10. For Soil EC, statistically significant differences were observed both between treatments (F4, 12=3.28, p = 0.049 - a marginal effect) and over time (F3, 45=8.59, p=0.0001). Predicted means and standard errors for each significant main effect are shown FIGS. 11 and 12. For ammonium acetate (AA) extractable nickel, statistically significant differences were observed both between treatments (F4, 12=5.66, p = 0.008) and over time (F3, 45=10.03, p<0.0001). Predicted means and standard errors for each significant main effect is shown in FIGS. 13 and 14. For ammonium acetate extractable magnesium, a statistically significant interaction effect was found between treatment and sampling date (F12,45=2.27, p=0.02). Overall, the largest effect is attributed to differences over time (F3, 45=6.81, p=0.007). Predicted means and standard errors are shown in FIG. 15. A multivariate correlation figures between all soil data can be seen in FIG. 16. \|[0140] The above preliminary data was collected over the first 8 months of the field trial experiment. Additional data will be gathered until 12 months after the start of the field trial experiment to further elucidate the relationship between the application rate of the weatherable rock and the accumulation of metal by the hyperaccumulator plant, the soil pH, the soil electrical conductivity, the weatherable rock-derivable cations in the soils and plants, and the heavy metals in the soils and the plants, as well as determining the weathering rate of the weatherable rock, the amount of nickel ore extractable from the plants, and quantifying the amount of carbon dioxide sequestered. \|Example 3: Field-scale enhanced rock weathering experiment with two controls\|[0141] In this example, a field- scale trial is employed to further investigate the synergistic combination of nickel phytomining and enhanced weathering. A scale diagram of the randomized complete block design used in the trial is shown in FIG. 17. The trial uses an approximately level 112 m x 208 m field site that is divided into four blocks of equivalent area, each measuring 56 m x 104 m, with every block subdivided into 10 randomly-assigned 12 m x 18 m plots representing the ten treatments as shown in FIG. 17. The amount of rock treatment added to each plot as measured in tonnes of serpentinite rock per hectare is shown in FIG. 17. Neither rock nor hyper- accumulator plants are added to the plots marked with ‘XX’ in FIG. 17. These plots are designed to simulate native soil conditions. The plots are segregated by an 8 m margin of untreated land. \|[0142] Two control treatments are included in this study: a rock-free control (i.e. 0 tonnes of rock added per hectare) where hyperaccumulator plants are grown, and a second control where no plants, rock amendments, or management practices are employed, as denoted by ‘XX’ in FIG. 5. The rock-free control is used to assess the effect of different rock applications on nickel uptake efficiency and carbon capture. The experiments with no plants, rock amendments, or management practices control serves a baseline (the native soil’s background conditions). \|Soil sample collection and measurements \|[0143] Following a W-shaped sampling pattern, multiple baseline soil samples are collected and aggregated from each of the forty plots at three discrete depths (0-0.3, 0.3-0.6 and 0.6-0.9 m) using a steel auger. These initial soil samples are separately homogenized, passed through a 2-mm mesh size sieve, and air-dried. Soils are then tested for pH (in H2O and IM KC1) and electrical conductivity (in H2O); inorganic/organic carbon and nitrogen %; plant-available nitrogen, phosphorus and potassium; soil texture (sand/silt/clay %), bulk density and water holding capacity; cation exchange capacity and exchangeable acidity; major oxide and soil mineralogy %; and, total and plant-available Ca, Mg, K, Na, Fe, Cd, Co, Cr, Cu, Mn, Ni, Pb, and Zn. Further soil samples are taken at bi -monthly intervals and tested to determine changes in fundamental soil parameters (pH, electrical conductivity, organic/inorganic carbon) and the concentration of exchangeable (plant- available) metals. These data are critical for monitoring changes in nickel availability and carbon dioxide capture rates in the plots. \|Plant sample collection and measurements \|[0144] Approximately 1-year after the start of the field trial, shoot tissues are harvested from all plots, and the shoot tissues are dried and weighed to quantify crop performance. In addition, plant materials are powdered, digested, and tested to determine metal content and analyze the correlation between rock application rate and nickel uptake efficiency. Total plant calcium, magnesium, potassium, and sodium values are added to the respective values from the soil analyses of exchangeable elements, which together enable the quantification of rock weathering and carbon capture rates. \|Aqueous sample collection and measurements \|[0145] Pore water samples are extracted from the soil using lysimeters installed in the plots. These aqueous samples are analyzed for changes in the following parameters: pH, electrical conductivity, and alkalinity; and dissolved cations (e.g. nickel, magnesium) and anions (e.g. chloride, nitrate). These data are essential for accurate monitoring of rock dissolution, nickel release, and carbon capture rates. Soil-atmosphere greenhouse gas sample collection and measurements \|[0146] Gaseous samples are collected during the trial using static chambers installed in the plots and are analyzed using gas analysis mass spectrometry to determine soil-atmosphere fluxes of major greenhouse gasses, such as carbon dioxide, methane, and nitrous oxide. This example seeks to determine the effects of the addition of alkaline rocks to the soil on overall emissions of potent non-CCh greenhouse gasses, and thus impact on climate change. These gas measurements are performed in serpentine soils, and also provide evidence that the soil amendments and agricultural management practices associated with the trial result in the conversion of existing soil organic carbon into atmospheric carbon dioxide. \|Example 4: Life Cycle Assessment at Kilotonne and Megatonne Scales Per Year\|[0147] A Life Cycle Assessment (LCA) was employed to ensure that the enhanced rock weathering/hyperaccumulator plant operation is sufficiently CO2 negative at the necessary scale. The aim was to model the net sequestration of 1 kilotonne and 1 megatonne of CO2 per year. The LCA was conducted using SimaPro software which draws data from various databases. The study adopted a cradle-to-gate approach, which includes all the major processes in the life cycle from the mining operation to the production of nickel ore, however the environmental impact of waste treatment was excluded from the LCA due to the ambiguity of its relevance. The two products of the operation are CO2 uptake (carbon dioxide removal through enhanced rock weathering) and the production of nickel ore through phytomining. The major processes within the established system boundaries include the mining, crushing, and milling of serpentine, the transportation of the serpentine rock to the site of placement, the fertilizer used, and harvesting, drying, and combustion of the hyperaccumulator plants. A unit area of land was used as the functional unit for the LCA to account for both the CO2 extraction and the nickel ore production. For example, per every m2 of area of serpentine soil used for the cultivation of A. Murale (or a similar hyperaccumulator plant), a certain amount of nickel will be produced and a certain amount of CO2 will be sequestered. This functional unit ensures that neither of the two products of the system (i.e. CO2 uptake and the production of nickel ore) are neglected from the LCA analysis and that their amounts are calculated independently of each other. \|[0148] The data used for the LCA was collected from several sources and the model was built on the basis of existing models. The data related to standard transportation, machinery, energy, and materials were kept as they were in the models, apart from several necessary adjustments to bring the model closer in line with the operation. For example, during the whole process, the electricity comes from the grid, where it is mostly produced using hydropower. This feature was reflected in the model. It is not required that hydropower be utilized in the process, though it will lower the net negative efficiency. A range of parameters, such as the weathering rate and serpentine content in soil, was introduced into the model. The information used to determine the parameter values was sourced from a combination of existing literature on similar experiments with hyperaccumulators and mineral weathering. The firm relied on rates of natural weathering processes which resulted in calculations that predict significant CO2 uptake and nickel production. \|[0149] The models for 1 kilotonne-scale production yearly can be seen in FIG. 18. The 1 megatonne-scale chart can be seen in FIGS. 19A and 19B. The main difference between the operations is the increased transport distance between the serpentine mining site and the farming sites in the megatonne- scale model as compared to thel kilotonne-scale model. Although not incorporated into the model, utilizing renewable energy for transportation of the rock between the mining site and farming sites would help ensure that the process remains CO2 negative even with long transportation distances. According to this LCA study, the operation can run at scale at an approximately 90% net efficiency in terms CO2 sequestration; additional details of the LCA study can be found in FIG. 20.	(WO2024/020548)\| METHODS FOR OBTAINING CARBON NEUTRAL OR CARBON NEGATIVE METALS FROM PLANTS, AND RELATED COMPOSITIONS \|CROSS-REFERENCE TO RELATED APPLICATIONS \|[0001] This application claims priority to and benefit of U.S. Provisional Application Serial No. 63/391,662, filed July 22, 2022, which is incorporated by reference in its entirety. \|FIELD \|[0002] The present disclosure relates generally to methods of extracting metals from rocks and sequestering carbon dioxide, and more specifically to methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. \|BACKGROUND \|[0003] Carbon dioxide is the dominant greenhouse gas released by human activities and the major contributor to global warming. Carbon sequestration is the process of capturing and storing atmospheric carbon dioxide. It is the only approach that humans can use to actively reduce the amount of carbon dioxide in the atmosphere. Currently, two main types of carbon sequestration are geologic carbon sequestration and biologic carbon sequestration. Current methods for sequestering carbon dioxide, such as underground sequestration, generally face problems related to economic viability, carbon dioxide leakage, and potential contamination of groundwater. Accordingly, there exists a need in the art for cost-effective methods to remove carbon dioxide from the atmosphere at a gigatonne scale while minimizing the negative impacts on the environment. \|BRIEF SUMMARY \|[0004] In some aspects, provided herein are methods and systems that combine enhanced weathering and phytomining to not only sequester carbon dioxide but also extract metals from surrounding soil. Enhanced weathering, which includes terrestrial enhanced weathering and oceanic enhanced weathering, is weathering accelerated by spreading finely ground silicate rock onto surfaces. This helps to accelerate chemical reactions between rocks, water and air. Phytomining refers to the use of hyperaccumulator plant species to concentrate metals from soils and subsequently processing the hyperaccumulator biomass to generate useful metal products. Hyperaccumulators are rare plants that draw up metal from the soil on which they grow, and accumulate high levels of metals in their biomass.\|[0005] In some embodiments, the metals may comprise nickel, cobalt, chromium or any combination thereof. In some embodiments, the methods and systems provided sequester carbon dioxide through a chemical weathering process that results in the release of Mg2+ ions. In some embodiments, the metals are phytomined from serpentinite. Serpentinite is a rock comprising one or more of the serpentine group minerals. Minerals in this group are rich in magnesium and iron. Serpentinite has been called serpentine or serpentine rock, particularly in older geographical texts and in wider cultural settings. In some embodiments, serpentinite is a rock comprising one or more of the serpentine group minerals. In some embodiments, serpentinite is a rock comprising one or more minerals having the chemical formula D3[Si2Os](OH)4, wherein D is selected from the group consisting of Mg, Fe, Ni, Mn, Al, and Zn. In some embodiments, serpentinite is a rock comprising one or more mineral selected from the group consisting of amesite, antigorite, berthierine, brindleyite, caryopilite, chrysotile, cronstedtite, fraipontite, guidottiite, kellyite, lizardite, nepouite, and pecoraite. \|[0006] In some embodiments, the methods and systems provided utilize plant species that are tolerant to soils having high metal contents. In some embodiments, the plants are tolerant of high pH soils. In some embodiments, the plants are tolerant of low nutrient soils. In some embodiments, the plants are hyperaccumulators of nickel. In some variations, provided is a method comprising transporting weatherable rock from a quarry, using mechanical activation to grind the weatherable rock to particles to increase reactive mineral surface area, dispersing the weatherable rock particles into the soil within a plot of land, planting nickel hyperaccumulating plants onto the plot of land to capture the nickel released from the weatherable rock during chemical weathering. In some embodiments, the presence of the nickel hyperaccumulating plants accelerates the chemical weathering of the weatherable rock. In some embodiments, the nickel hyperaccumulating plants may be harvested and further processed to yield a purified nickel composition. In some embodiments, the weatherable rock is ground to a particle size suitable to optimize both the rate of chemical weathering and the rate of nickel accumulation in the hyperaccumulating plant. In some embodiments, grinding the rock to particles comprises grinding the rock to a size of between about 1 pm and about 10 cm. In some variations of the foregoing, the weatherable rock comprises serpentine. In some variations of the foregoing, the weatherable rock comprises serpentinite. \|[0007] In some embodiments, the nickel may be nickel metal in oxidation state 0, or any suitable nickel salts and nickel complexes, such as Ni2+ salts. In some variations, the nickel is a Ni2+ salt or complex. In some embodiments, the nickel may be in an oxidation state of -1, 0, 1, 2, 3, or 4, or any combination thereof. \|[0008] In some variations, the weatherable rock may be obtained from the tailings, waste, or overburden from traditional nickel mines. In some embodiments, the weatherable rock comprises serpentine. In some embodiments, the nickel hyperaccumulating plants are directly irrigated. In some embodiments, the irrigation is accomplished using a continuous irrigation system. In some embodiments, the irrigation is accomplished using an automated irrigation system. \|[0009] In some variations, the methods and systems employ hyperaccumulator plants that are capable of growing in high and even pure levels of serpentine and that are be able to survive and accelerate the weathering rate of the serpentine minerals, especially when fertilized and irrigated. \|[0010] In one aspect, provided is a method for obtaining nickel metal, comprising mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium, and at least 0.1% by weight of nickel to provide a particulate weatherable rock composition, combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil, harvesting the nickel hyperaccumulator plant, and processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel. \|[0011] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash comprising at least 5% nickel by weight, and refining the nickel-enriched ash composition to provide a substantially pure nickel. \|[0012] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises heat treating the harvested nickel hyperaccumulator plant to provide a nickel- enriched ash comprising at least 5% nickel by weight, and refining the nickel-enriched ash composition to provide a substantially pure nickel. \|[0013] In certain embodiments, Mg2+ is leached from the weatherable rock-enriched soil at a rate faster than the observed rate of stationary ultramafic minerals, or minerals without plants growing in them. In certain embodiments, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the nickel hyperaccumulator plant is growing. \|[0014] In other variations, the method may be employed for obtaining one or more metals, including nickel, cobalt, chromium or any combination thereof. In variations where a plurality of metals are obtained, multiple hyperaccumulator plants suitable for harvesting the metals are employed in the process. For example, in some variations of the methods, a nickel hyperaccumulator plant and a cobalt hyperaccumulator plant are used in the weatherable rock-enriched soil to harvest a combination of nickel and cobalt. \|[0015] In some embodiments, at least 10 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. \|[0016] In some embodiments, the weatherable rock comprises ultramafic rock. In some embodiments, the weatherable rock comprises mafic rock. In some embodiments, the weatherable rock comprises less than about 55% silica by weight. In some embodiments, the weatherable rock comprises less than about 45% silica by weight. In some embodiments, the weatherable rock comprises between about 45% and about 55% silica by weight. In some embodiments the weatherable rock comprises one or more minerals selected from the serpentine group. In some embodiments, the weatherable rock comprises olivine. In some embodiments, the weatherable rock comprises serpentinite. In some embodiments, the weatherable rock comprises gabbro or basalt, or a combination. In some embodiments, the weatherable rock comprises a combination of mafic rocks or minerals. \|[0017] In some embodiments, the method comprises mining the weatherable rock. In some embodiments, the method comprises transporting the mined weatherable rock from a mining location to a grinding location. In some embodiments, the method comprises mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock. \|[0018] In some embodiments, the particulate weatherable rock composition has a particle size between 1 pm and 10 cm. In some embodiments, the weatherable rock-enriched soil comprises between 10% and 100% particulate weatherable rock composition by weight. \|[0019] In some embodiments, the nickel hyperaccumulator plant is a plant belonging to the genus Odontarrhena. In some embodiments, the nickel hyperaccumulator plant is grown inside of a greenhouse. In some embodiments, the nickel hyperaccumulator plant is grown under polyethylene film (e.g., a polytunnel). \|[0020] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil. In some embodiments, the pH of the weatherable rock-enriched soil is at least 7. In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises intermittently irrigating the weatherable rock-enriched soil. \|[0021] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises fertilizing the plant. In some embodiments, nitrogen, phosphorus, and potassium (NPK) fertilizers are used to fertilize the plant. In some embodiments, calcium is added to the soil. In some embodiments, boron is used to stimulate flowering in the plant. In some embodiments, soil analysis is used to determine which nutrients are lacking in the soil. In some such embodiments, fertilizer is used to provide the plant with one or more of the nutrients that are determined as lacking in the soil. In some embodiments, exogenous additives are used to increase the available levels of metals in the soil. In some embodiments the exogenous additive comprises citric acid. In some embodiments, potassium is added to the soil. In some embodiments, sulphur-containing compounds are added to the soil. \|[0022] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprises drying the nickel hyperaccumulator plant to provide a dried biomass composition, crushing the dried biomass composition to provide a crushed biomass composition, and burning the crushed biomass composition to provide a nickel-enriched ash composition. \|[0023] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises directly leaching the harvested nickel hyperaccumulator plant using sulfuric acid to provide an acid leachate; purifying the acid leachate using column chromatography to provide a Ni-enriched acid leachate; and further processing the Ni-enhanced acid leachate to provide a substantially pure nickel. \|[0024] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises leaching the nickel-enriched ash composition to provide a leachate; recovering nickel from the leachate using solvent extraction or an ion exchange resin to obtain a recovered nickel composition; and purifying the recovered nickel composition using electrowinning to obtain a substantially pure nickel. \|[0025] It should be understood that, in other variations, the embodiments of the method described above for harvesting nickel may be modified to harvest one or more other metals, such as cobalt and chromium, or any combinations of such metals. \|[0026] In some embodiments, refining the nickel-enriched ash composition comprises: acid leaching the nickel-enriched ash composition to provide an acid leachate; neutralizing the acid leachate with Ca(OH)2 to provide a first treated leachate; adding NaF to the neutralized leachate to provide a second treated leachate; adding ammonium sulfate to the second treated leachate to provide a third treated leachate; drying the third treated leachate to provide ammonium Ni sulfate hexahydrate (ANSH); and processing the ANSH to obtain a substantially pure nickel. \|[0027] In some embodiments, the method further comprises quantifying the amount of carbon dioxide that is released or sequestered in one or more steps of the method. \|[0028] In another aspect, provided is nickel metal prepared according to any of the foregoing methods. \|[0029] In another aspect, provided is a processed nickel composition comprising substantially pure nickel, and one or more of the following: (i) precipitated gypsum, (ii) one or more low weight carboxylic acids, (iii) one or more Ni-containing compounds selected from the group consisting of NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, nickel oxalate, and nickel sulfate, or (v) one or more carbonates selected from the group consisting of K2CO3, CaCO3, K2Ca(CO3)2. \|[0030] In another aspect, provided is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: (i) one or more elements selected from the group consisting of Ca, Fe, K, Mg, P, C, H, N, and O, (ii) one or more carbonates selected from the group consisting of K2CO3, CaCO3, K2Ca(CO3)2, (iii) plant cells, (iv) hydroxyapatite or oxyhydroxyapatite, or (v) one or more oxides selected from the group consisting of NiO, CaO, MgO, and MgNiO2.\|[0031] In yet other aspects, provided is a metal-enriched ash obtained by any of the methods described herein. In some variations, the metal is nickel, cobalt, or chromium, or a combination thereof. \|DESCRIPTION OF THE FIGURES \|[0032] The present application can be understood by reference to the following description taken in conjunction with the accompanying figures. \|[0033] FIG. 1 depicts an exemplary process for obtaining metal using weatherable rock and phytomining. \|[0034] FIG. 2 depicts the different growing conditions employed in the assessment of weathering rates for different soil and plant configurations. \|[0035] FIG. 3 depicts the total amount of magnesium leached under each of the conditions of FIG. 2 over the course of 4 months. \|[0036] FIGS. 4 depicts a diagram of an exemplary field- scale randomized complete block design used to investigate the synergistic combination of nickel phytomining and enhanced weathering. \|[0037] FIG. 5 depicts the pH analysis of topsoils for five application rates approximately eight months after crushed serpentinite rock was applied. \|[0038] FIG. 6 depicts the electrical conductivity analysis of topsoils for five application rates approximately eight months after crushed serpentinite rock was applied. \|[0039] FIG. 7 depicts the amount of nickel in the shoot tissues of hyperaccumulator plants grown on soils treated with eight different application rates of serpentinite rock. \|[0040] FIG. 8 depicts the results from a time-series analysis of topsoil Ni concentrations for five application rates using a Mehlich 1 reagent. \|[0041] FIGS. 9 and 10 depicts the results of statistical analysis of the pH of the soil with respect to application rate and sampling time, respectively. \|[0042] FIGS. 11 and 12 depicts the results of statistical analysis of the electrical conductivity of the soil with respect to application rate and sampling time, respectively.\|[0043] FIGS. 13 and 14 depicts the results of statistical analysis of the ammonium acetate extractable nickel content of the soil with respect to application rate and sampling time, respectively. \|[0044] FIG. 15 depicts the results of statistical analysis of the ammonium acetate extractable magnesium content of the with respect to application rate and sampling time. \|[0045] FIG. 16 depicts a multivariate correlation of the statistical analysis of the soil data. \|[0046] FIG. 17 depicts a diagram of another exemplary field-scale randomized complete block design used to investigate the synergistic combination of nickel phytomining and enhanced weathering. \|[0047] FIG. 18 depicts the life cycle assessment model for an exemplary 1 kilotonne-scale production. \|[0048] FIGS. 19A and 19B depict the life cycle assessment model for an exemplary 1 megatonne-scale production. \|[0049] FIG. 20 depicts additional data used in the life cycle assessment of an exemplary process. \|DETAILED DESCRIPTION \|[0050] The following description sets forth exemplary compositions, methods, systems, parameters and the like. It should be recognized, however, that such description is not intended as a limitation on the scope of the present disclosure but is instead provided as a description of exemplary embodiments. \|[0051] In one aspect, provided herein is a method of sequestering carbon dioxide comprising providing a weatherable rock comprising one or more metals, subjecting the weatherable rock to conditions sufficient to cause the rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the one or more metals, and wherein the alkalinity facilitates the sequestration of carbon dioxide through the conversion of carbon dioxide to bicarbonate or carbonate, and extracting and processing the released metals to provide a metal-enriched composition. In some embodiments, the conditions cited above comprise growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock. In some embodiments, the conditions comprise growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock and continuously irrigating the one or more metal hyperaccumulator plants using a drip irrigation system. In some embodiments, the extracting and processing the released one or more metals comprises growing one or more metal hyperaccumulator plants in a medium comprising the weatherable rock, wherein the one or more metal hyperaccumulator plants accumulate the released one or more metals. In some embodiments the extracting and processing the released one or more metals further comprises processing the metal hyperaccumulator biomass using any suitable technique known in the art to prepare a metal-enriched composition. In some embodiments, the one or more metals comprise a heavy metal. In some embodiments, the one or more metals comprise a toxic metal. In some embodiments, the one or more metals comprise a metal selected from the group consisting of Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the one or more metals comprise cobalt. In some embodiments, the one or more metals comprise chromium. In some embodiments, the one or more metals comprise nickel. In some embodiment the one or more metals comprise any metal that can be hyperaccumulated by a hyperaccumulator plant. In some embodiments, providing the weatherable rock comprises mining the weatherable rock. In some embodiments, providing the weatherable rock further comprises mechanically processing the weatherable rock to reduce the particle size of the weatherable rock to between about 1 pm and about 10 cm. In some embodiments, providing the weatherable rock further comprises admixing the weatherable rock with one or more additional growing media including, for example, soil. \|[0052] In one aspect, provided herein is a method of sequestering carbon dioxide comprising providing a weatherable rock comprising a metal, subjecting the weatherable rock to conditions sufficient to cause the rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide through the conversion of carbon dioxide to bicarbonate or carbonate, and extracting and processing the released metal to provide a metal-enriched composition. In some embodiments, the conditions cited above comprise growing a metal hyperaccumulator plant in a medium comprising the weatherable rock. In some embodiments, the conditions comprise growing a metal hyperaccumulator plant in a medium comprising the weatherable rock and continuously irrigating the metal hyperaccumulator plant using a drip irrigation system. In some embodiments, the extracting and processing the released metal comprises growing a metal hyperaccumulator plant in a medium comprising the weatherable rock, wherein the metal hyperaccumulator plant accumulates the released metal. In some embodiments the extracting and processing the released metal further comprises processing the metal hyperaccumulator biomass using any suitable technique known in the art to prepare a metal-enriched composition. In some embodiments, the metal is a heavy metal. In some embodiments, the metal is a toxic metal. In some embodiments, the metal is selected from the group consisting of Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the metal comprises cobalt. In some embodiments, the metal comprises chromium. In some embodiments, the metal comprises nickel. In some embodiment the metal is any metal that can be hyperaccumulated by a hyperaccumulator plant. \|[0053] In some embodiments, the weatherable rock comprises a magnesium-bearing silicate mineral. In certain embodiments, the magnesium-bearing silicate mineral is in the olivine mineral group. In certain embodiments, the magnesium-bearing silicate mineral is in the serpentinite mineral group. In other variations, any combination of suitable weatherable rocks described herein may be used. \|[0054] In some embodiments, providing the weatherable rock comprises mining the weatherable rock. In some embodiments, providing the weatherable rock further comprises mechanically processing the weatherable rock to reduce the particle size of the weatherable rock to between about 1 pm and about 10 cm. In some embodiments, providing the weatherable rock further comprises admixing the weatherable rock with one or more additional growing media including, for example, soil. \|[0055] In another aspect, provided herein is a method that utilizes plants that are not only tolerant to serpentine, but that evolved especially to live in high alkalinity (e.g., high pH) soils, composed of high percentages of low nutrient and metal heavy soils. These plants that typically take up nickel as a means of protection can be utilized to produce commercial yields of nickel. In certain aspects, provided is a method to bring fresh serpentine-containing rock from nearby quarries, utilizing mechanical activation to grind them to particles, for example micron-sized particles, to increase the reactive surface area, then transported to fields where nickel hyperaccumulating plants have been planted to capture the nickel release from the soil, and also accelerate the release of magnesium ions from the crystal lattice of the serpentine in order to increase the amount of carbon sequestered when those ions run off to the ocean. The methods provided herein overcome the previous blockers that prevented the deployment of terrestrial enhanced weathering for the purposes of carbon removal, and by increasing the revenue streams available to the process are able to make direct and intentional phytomining possible. The methods provided make phytomining a primary mining technique. In some variations, the methods can also use tailings, waste, or overburden from traditional nickel mines. In certain variations, the methods involve actively grinding minerals to below a certain size in order to specifically increase the reactive surface area. Further, in some variations, direct irrigation can be utilized to both enhance the weathering rate, and increase the plant growth, the plant then releases acids that further break down the rocks, releasing magnesium that leads to carbon removal and drawing nickel into the plants, preventing its release into the environment. \|[0056] In some variations of the foregoing, the chemical weathering process results in the formation of new soil minerals. In certain variations of the foregoing, the chemical weathering process results in fully weathered rock. In some embodiments, the weathering process results in fully weathered rock within about 20 years; or between 1 year and 20 years; or within about 1 year, about 2 years, about 3 years, about 4 years, about 5 years, about 6 years, about 7 years, about 8 years, about 9 years, about 10 years, about 11 years, about 12 years, about 13 years, about 14 years, about 15 years, about 16 years, about 17 years, about 18 years, about 19 years, or about 20 years. \|[0057] With reference to FIG. 1, depicted is an exemplary process 100 for obtaining metal using weatherable rock and phytomining. Step 102 involves mechanically grinding a weatherable rock to provide a particulate weatherable rock composition. In step 104, the particulate weatherable rock composition is combined with a soil to provide a weatherable rock-enriched soil. In step 106, a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil is grown. Then, in step 108, the metal hyperaccumulator plant is harvested. In step 110, the harvested metal hyperaccumulator plant is processed using any suitable techniques or methods known in the art to provide a substantially pure metal. In some variations of the process, step 110 may be optional. For example, in certain variations, the process described herein does not require harvesting of the metal from the plant to obtain a substantially pure metal. In other variations, the process further includes harvesting of the metal from the plant to obtain a substantially pure metal.\|[0058] Thus, in some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising magnesium, and a metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil; harvesting the metal hyperaccumulator plant; and processing the harvested metal hyperaccumulator plant to provide a substantially pure metal. In some embodiments, processing the harvested metal hyperaccumulator plant comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide a substantially pure metal by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide a substantially pure metal may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 20% by weight of magnesium and 0.1% by weight of the metal. In some embodiments, the metal-enriched ash comprises at least 5% of the metal by weight. \|[0059] In some embodiments, provided is a method for preparing one or more metals comprising mechanically grinding a weatherable rock comprising magnesium, and one or more metals to provide a particulate weatherable rock composition; either combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil or using the particulate weatherable rock composition directly as a weatherable rock- enriched soil without combining it with any additional media; growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil, wherein each of the one or more plants is a hyperaccumulator of at least one of the one or more metals; harvesting the one or more metal hyperaccumulator plants; and processing the one or more harvested metal hyperaccumulator plants to provide one or more substantially pure metals. In some embodiments, processing the one or more harvested metal hyperaccumulator plants comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide one or more substantially pure metals by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide one or more substantially pure metals may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 20% by weight of magnesium and 0.1% by weight of each of the one or more metals. In some embodiments, the metal-enriched ash comprises at least 5% of each of the one or more metals by weight.\|[0060] In some embodiments, provided is a method for obtaining one or more substantially pure metals comprising mechanically grinding a weatherable rock comprising at least 20% by weight of magnesium and at least 0.1% by weight of each of the one or more metals to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil, wherein each of the one or more plants is a hyperaccumulator of at least one of the one or more metals; harvesting the one or more metal hyperaccumulator plants; and processing the one or more harvested metal hyperaccumulator plants to provide one or more substantially pure metals. \|[0061] In some variations, substantially pure metal refers to a metal that is at least 90%, at least 95%, at least 96%, at least 97%, at least 98%, at least 99%, at least 99.9%, at least 99.99%. at least 99.999%, or at least 99.9999% pure by weight. \|[0062] In some embodiments, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the metal hyperaccumulator plant is growing. In some embodiments, about 10% of the Mg by weight is weathered per year. In some embodiments, about 90% of the Mg by weight is weathered per month. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated over a period of about 20 years. In some embodiments, at least about 90% of the weatherable Mg2+ ions by weight are liberated over a period of less than about 20 years. In any of the foregoing embodiments, the weight of Mg2+ refers to the weight of the magnesium component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts that the Mg2+ is a part of. \|[0063] In some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising calcium and a metal to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a plant that is a hyperaccumulator of the metal in the weatherable rock-enriched soil; harvesting the metal hyperaccumulator plant; and processing the harvested metal hyperaccumulator plant to provide a substantially pure metal. In some embodiments, processing the harvested metal hyperaccumulator plant comprises ashing the harvested metal hyperaccumulator plant to provide a metal-enriched ash and refining the metal-enriched composition to provide a substantially pure metal by weight. In some embodiments, processing the harvested metal hyperaccumulator plant to provide a substantially pure metal may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 10% by weight of calcium and at least 0.1% by weight of the metal. In some embodiments, the metal-enriched ash comprises at least 5% of the metal by weight. \|[0064] In some embodiments, Ca2+ is leached at a rate of at least 1% by weight of the total Ca2+ in the weatherable rock per year from the weatherable rock-enriched soil while the metal hyperaccumulator plant is growing. In some embodiments, about 10% of the Ca by weight is weathered per year. In some embodiments, about 90% of the Ca by weight is weathered per month. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated over a period of about 20 years. In some embodiments, at least about 90% of the weatherable Ca2+ ions by weight are liberated over a period of less than about 20 years. In any of the foregoing embodiments, the weight of Ca2+ refers to the weight of the calcium component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts that the Ca2+ is a part of. \|[0065] In some embodiments, the rate at which Mg2+ is leached is measured by measuring the concentration of the Mg2+ in the water used to irrigate the hyperaccumulator plant. In some embodiments, the rate at which Ca2+ is leached is measured by measuring the concentration of Ca2+ in the water used to irrigate the hyperaccumulator plant. \|[0066] In some variations of the foregoing, the weatherable rock comprises between 0.01% and 20% of the metal by weight. In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of the metal by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of the metal. \|[0067] In some embodiments, the metal comprises Ni, Cr, Co, Al, Ag, Cu, Mn, Mo, Hg, Mo, Pb, or Zn, or any combination thereof. In some embodiments, the metal comprises a rare earth metal. In some embodiments, the metal comprises nickel. In some embodiments, the metal comprises cobalt. In some embodiments, the metal comprises chromium. In some embodiments, the metal is a metal that can be hyperaccumulated by a hyperaccumulator plant. In some embodiments, the metal is a metal found in a weatherable rock. In some embodiments, the metal is a metal found in a weatherable rock that can be hyperaccumulated by a hyperaccumulator plant. \|[0068] In some embodiments, provided is a method for preparing a metal comprising mechanically grinding a weatherable rock comprising magnesium and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; liberating nickel from the weatherable rock by subjecting the weatherable rock-enriched soil to conditions sufficient to cause the weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein acid is not added to the weatherable rock- enriched soil; growing a plant that is a hyperaccumulator of nickel in the weatherable rock- enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide substantially pure nickel. \|[0069] In some embodiments, the amount of carbon dioxide emitted from the weathering of the weatherable rock is less than amount of carbon dioxide sequestered from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide emitted from the weathering of the weatherable rock, harvesting the nickel hyperaccumulator plant, and processing the harvested nickel hyperaccumulator plant is less than amount of carbon dioxide sequestered from the weathering of the weatherable rock. \|[0070] In some embodiments, provided is a method for preparing nickel metal comprising mechanically grinding a weatherable rock comprising magnesium, and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel. In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash and refining the nickel-enriched composition to provide a substantially pure nickel by weight. In some embodiments, processing the harvested nickel hyperaccumulator plant to provide a substantially pure nickel may be accomplished using any suitable techniques known in the art. In some embodiments, the weatherable rock comprises at least 10% by weight of magnesium and at least 0.1% by weight of nickel. In some embodiments, the nickel-enriched ash comprises at least 5% nickel by weight. \|[0071] In some variations of the foregoing, Mg2+ is leached at a rate of at least 1% by weight of the total Mg2+ in the weatherable rock per year from the weatherable rock-enriched soil while the nickel hyperaccumulator plant is growing. \|[0072] In some variations of the foregoing, the weatherable rock comprises between 5% and 60% Mg by weight. In some embodiments, the weatherable rock comprises between 25% and 50% Mg by weight. In some embodiments, the weatherable rock comprises about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, or about 70% Mg by weight. \|[0073] In some variations of the foregoing, the weatherable rock comprises between 5% and 60% Ca by weight. In some embodiments, the weatherable rock comprises between 25% and 50% Ca by weight. In some embodiments, the weatherable rock comprises about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, or about 70% Ca by weight. \|[0074] In some variations of the foregoing, the weatherable rock comprises between 0.01% and 20% of nickel by weight. In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of nickel by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of nickel. \|[0075] In some variations of the foregoing, the weatherable rock comprises nickel and Mg. In some embodiments, the weatherable rock comprises between 0.01% and 25% of nickel by weight and between 5% and 60% of Mg by weight. In some embodiments, the weatherable rock comprises between 0.01% and 25% of nickel by weight and between 25% and 50% of Mg by weight. \|[0076] In some embodiments, the weatherable rock comprises between 0.2% and 0.4% of nickel by weight. In some embodiments, the weatherable rock comprises at least about 0.2% metal by weight. In some embodiments, the weatherable rock comprises about 0.01%, about 0.1%, about 0.2%, about 0.3%, about 0.4%, about 0.5%, about 0.6%, about 0.7%, about 0.8%, about 0.9%, about 1%, about 2%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, or about 25% by weight of nickel. \|[0077] In some variations of the foregoing, the nickel-enriched ash composition comprises between 1% and 99.8% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 1% and 35% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 1% and 30% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 30% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 20% nickel by weight. In some embodiments, the nickel-enriched ash composition comprises between 0.1% and 15% nickel by weight. In some embodiments, the nickel- enriched ash composition comprises about 0.1%, about 0.5%, about 1%, about 1.5%, about 2%, about 2.5%, about 3%, about 4%, about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, or about 40% nickel by weight. \|[0078] In some variations of the foregoing, refining the nickel-enriched composition provides a nickel that is at least 15%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 98%, at least 99%, at least 99.9%, at least 99.9%, at least 99.99%, at least 99.999%, or at least 99.9999% pure by weight. In some embodiments, refining the nickel-enriched composition provides a nickel that is between 15% and 100% pure by weight. \|[0079] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprises drying the nickel hyperaccumulator plant to provide a dried biomass composition, crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a nickel-enriched ash composition. In some embodiments, the ashing is performed at a temperature of about 500 °C. \|[0080] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises directly leaching the harvested nickel hyperaccumulator plant to provide a leachate; purifying the leachate to provide a Ni-enriched leachate; and further processing the Ni-enhanced leachate to provide a substantially pure nickel. In some embodiments, the direct leaching is performed using a hydrothermal process. In some embodiments, the direct leaching is performed in acid. In some embodiments, the acid is sulfuric acid. In some embodiments, the acid is hydrochloric acid. In some embodiments purifying the leachate comprises purifying the leachate using column chromatography. In some embodiments purifying the leachate comprises purifying the leachate using solvent extraction. In some embodiments purifying the leachate comprises purifying the leachate using ion exchange chromatography. In some embodiments, further processing the Ni-enhanced leachate comprises electrowinning the nickel. \|[0081] In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash, leaching the nickel-enriched ash composition to provide a leachate, treating the leachate to provide ammonium Ni sulfate hexahydrate (ANSH), and processing the ANSH to obtain a substantially pure nickel. In some embodiments, the leaching is performed in acid. In some embodiments treating the leachate comprises neutralizing the leachate using a base to provide a first treated leachate, adding a fluoride source to the first treated leachate to provide a second treated leachate, adding ammonium sulfate to the second treated leachate to provide a third treated leachate, and drying the third treated leachate to provide ANSH. In some embodiments, the base is Ca(OH)2. In some embodiments, the fluoride source is NaF. In some embodiments, treating the leachate comprises purifying the ANSH via recrystallization. \|[0082] In some embodiments, provided is a method for preparing nickel catalysts comprising mechanically grinding a weatherable rock comprising magnesium, and nickel to provide a particulate weatherable rock composition; combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil; growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil; harvesting the nickel hyperaccumulator plant; and processing the harvested nickel hyperaccumulator plant to provide nickel catalysts. In some embodiments, processing the harvested nickel hyperaccumulator plant comprises ashing the harvested nickel hyperaccumulator plant to provide a nickel-enriched ash, leaching the nickel-enriched ash to provide a leachate, and further processing the leachate to provide nickel catalysts. In some embodiments, the ashing is performed at a temperature of 500 °C. In some embodiments, the leaching is performed in acid. In some embodiments, the acid is hydrochloric acid. In some embodiments, further processing the leachate to provide nickel catalysts comprises dispersing the leachate onto montromorillonite K10. In some embodiments, the weatherable rock comprises at least 10% by weight of magnesium and at least 0.1% by weight of nickel.\|[0083] In some embodiments, the amount of carbon dioxide sequestered is on the tonne scale for every tonne of nickel metal that is produced. In some embodiments, at least 1 tonne, at least 5 tonnes, at least 10 tonnes, at least 20 tonnes, at least 30 tonnes, or at least 40 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. In some embodiments, between 1 tonne and 100 tonnes, or between 10 tonnes and 100 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. In some embodiments, between 100 tonnes and 500 tonnes, or between 300 tonnes and 500 tonnes of carbon dioxide are sequestered for every tonne of nickel metal that is produced. \|[0084] In some embodiments, the weatherable rock comprises an ultramafic rock. In some embodiments, the weatherable rock comprises serpentine. In some embodiments, the weatherable rock comprises serpentinite. In some embodiments, the weatherable rock comprises olivine. In some embodiments, the weatherable rock contains less than 1% by weight of nickel. In some embodiments, the weatherable rock contains a metal that can be hyperaccumulated by a hyperaccumulator plant. \|[0085] In some embodiments, the method further comprises mining the weatherable rock. In other embodiments, the method further comprises transporting the mined weatherable rock from a mining location to a grinding location. \|[0086] In some embodiments, mechanically grinding the weatherable rock comprises crushing and/or milling the weatherable rock. In some embodiments, the energy used to mechanically grind the rock comes from renewable sources. \|[0087] In some embodiments, the particulate weatherable rock composition has an average particle size between about 1 pm and about 10 mm, between about 1 pm and about 10 cm, between about 1 pm and about 20 cm, between about 1 pm to about 5 mm, between about 1 pm to about 3 mm, or between about 100 pm to about 3 mm. \|[0088] In some embodiments, the weatherable rock-enriched soil comprises between 10% and 100%, between 70% and 100%, between 70% and 90%, between 70% and 80%, or between 80% and 90% particulate weatherable rock composition by weight. In certain embodiments, the weatherable rock-enriched soil comprises about 30%, about 40%, about 50%, about 60%, about 70%, about 80%, about 90%, or about 100% particulate weatherable rock composition by weight.\|[0089] In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of silicate rocks. In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of serpentinite rocks. In some embodiments, the weatherable rock-enriched soil is formed by natural weathering of olivine rocks. In some embodiments, natural weathering of serpentinite rocks results in weatherable rock-enriched soil with high nickel concentrations. \|[0090] In some embodiments, the nickel hyperaccumulator plant is a plant belonging to the genus Odontarrhena. In some embodiments the plant belongs to the genus Alyssum. In some embodiments the plant belongs to the family Brassicacaea. In some embodiments the plant belongs to the genus Bornmuellera. In some embodiments the plant belongs to the genus Thlaspi. In some embodiments, the plant is Alyssum Murale. In some embodiments, the plant is of the genus Odontarrhena. In some embodiments, the plant is Odontarrhena chalcidica. In some embodiments, the plant is Odontarrhena decipiens. In some embodiments, the plant is Berkheya coddii. In some embodiments, the plant is B. emarginata. In some embodiments, the plant is Stackhousia tryonii. In some embodiments, the plant is Phyllanthus balgooyi. In some embodiments, the plant is Rinorea bengalensis. In some embodiments, the plant may be a tree, bush, or vine. In some embodiments, the plant is a genetically modified plant. In some embodiments, the plant is any plant capable of hyperaccumulating a metal found in a weatherable rock. In some embodiments, the plant is any plant capable of hyperaccumulating nickel. In some embodiments, the plant is any hyperaccumulator plant species of the class known as a hypernickelophores, containing more than 1,000 pg Ni g 1. \|[0091] In some embodiments, the nickel hyperaccumulator plant is grown inside of a greenhouse. In some embodiments, the nickel hyperaccumulator plant is grown inside of a vertical farm. In some embodiments, the nickel hyperaccumulator plant is grown hydroponically. In some embodiments, the nickel hyperaccumulator plant is grown under a polyethylene film (e.g., a polytunnel). \|[0092] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the weathering rate of the weatherable rock. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the efficiency of nickel uptake by the plant. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the weathering rate of the weatherable rock and the efficiency of nickel uptake by the plant. \|[0093] In some embodiments, the environmental conditions of the weatherable rock- enriched soil are controlled to cause the weatherable rock to undergo a chemical weather process at an accelerated rate relative to natural chemical weathering environmental conditions. In some embodiments, the conditions cited above comprise growing one or more metal hyperaccumulator plants in the weatherable rock-enriched soil. In some embodiments, the conditions comprise growing one or more metal hyperaccumulator plants in a weatherable rock-enriched soil and continuously irrigating the one or more metal hyperaccumulator plants using a drip irrigation system. In some embodiments, the temperature, pH, irrigation, or bioactivity of the weatherable rock-enriched is controlled. \|[0094] In some embodiments, the rate of weathering of the weatherable rock is between about 0% and about 40% by mass of the weatherable rock between about 12 months and about 72 months from the date of combining the particulate weatherable rock composition with a soil to provide a weatherable rock-enriched soil and planting the hyperaccumulator plant in the weatherable rock-enriched soil. Any suitable methods known in the art may be used to determine the rate of weathering of the weatherable rock. For example, in one variation, the foregoing rates of weathering may be calculated using the Arrhenius equation. \|[0095] In some embodiments, the weathering rate is calculated by measuring the accumulation of rock-derived cations (e.g., Ca, Mg, Na, and K) in plant, soil, and/or aqueous effluent associated within a certain plot of land and subtracting the baseline amount of the corresponding cation measured in a corresponding control plot. For example, the net accumulation of Ca-cations due to mineral dissolution of weatherable rock can be calculated by subtracting the amount of Ca-cations measured in a control plot from the total amount of Ca-cations calculated by totaling the amount of Ca-cations in the water and/or effluent, the Ca-cations in plant tissues, and Ca-cations in the soil cation exchange pool. The amount of Ca-cations attributable to the weathering of weatherable rock can then be converted into spatially-averaged cation weathering rates (per unit of land area) or rates related to mineral surface area. In some embodiments, the weatherable rock is calculated in the number of moles of calcium, magnesium, sodium, and/or potassium released from the weatherable rock material into the soil per hectare of treated land per annum.\|[0096] In some embodiments, the weathering rate of the weatherable rock increases when the average particle size of the weatherable rock decreases. \|[0097] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to increase the weathering rate of the weatherable rock. In some embodiments, the environmental parameter that is optimized to increase the weathering rate of the weatherable rock is temperature. In some embodiments, the temperature of the surrounding air (e.g., climate) is increased to increase the weathering rate of the weatherable rock. In some embodiments, the temperature of the topsoil (e.g., where the weatherable rock is admixed into the soil) is increased to increase the weathering rate of the weatherable rock. In some embodiments, the amount of irrigation of the soil admixed with the weatherable rock is increased to increase the weathering rate of the weatherable rock. In some embodiments, the pH of the soil admixed with the weatherable rock is increased to decrease the weathering rate of the weatherable rock. In some embodiments, the pH of the soil admixed with the weatherable rock is decreased to increase the weathering rate of the weatherable rock. \|[0098] In some embodiments, the weathering rate of the weatherable rock is increased by increasing the amount of biological activity of the soil admixed with the weatherable rock. In certain embodiments, the increased biological activity of the soil is measured by the amount of carbon dioxide produced by the microbes per a given amount of the soil. In certain embodiments, the increased biological activity of the soil is measured by the amount of nitrogen-cycling and secretion of organic acids by plant roots and mycorrhizal fungi present in the soil. \|[0099] In some embodiments, increasing the concentration of Mg2+ ions in the soil admixed with the weatherable rock increases the weathering rate of the weatherable rock. In some embodiments, increasing the concentration of Ca2+ ions in the soil admixed with the weatherable rock increases the weathering rate of the weatherable rock. In certain variations, higher soil Ca and Mg content may decrease the weathering rate of rock material added to the soil, because chemical conditions in the groundwater may approach saturation for certain Ca- (and Mg-) bearing minerals. \|[0100] In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the accumulation of nickel by the plant. In some embodiments, the environmental conditions under which the nickel hyperaccumulator plant is grown are optimized to maximize the growth rate of the plant. In some embodiments, the humidity, temperature, or lighting of the environment in which the nickel hyperaccumulator plant is grown are controlled. In some embodiments, the nickel hyperaccumulator plant is grown in an outdoor field. \|[0101] In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to maximize the accumulation of nickel by the hyperaccumulator plant. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is between about 5 tonnes and 300 tonnes. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is between about 10 tonnes and 50 tonnes. In some embodiments, the amount of weatherable rock mixed into the soil to maximize the accumulation of nickel by the hyperaccumulator plant is about 37 tonnes. \|[0102] In some embodiments, the amount of nickel accumulated by a nickel hyperaccumulator plant increases proportionally with the amount of weatherable rock mixed into the soil in which the plant is grown. In some embodiments, increasing the amount of weatherable rock mixed in the soil does not result in an increase in the amount of nickel accumulated by a hyperaccumulator plant growing in the soil. In certain embodiments, high amounts of weatherable rock mixed into the soil result in high alkaline (e.g., high pH) soils which can negatively impact the mobility of the one or more metals released from the weatherable rock during the weathering process. \|[0103] In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown and the environmental conditions under which the hyperaccumulator plant is grown are optimized to control the pH of the soil. In some embodiments, the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to control the pH of the soil. In some embodiments, an increase in the pH of the soil decreases the mobility of the one or metals released by the weatherable rock mixed in the soil. In some embodiments, decreased mobility of the one or more metals in the soil results in lower accumulation of the metals by a hyperaccumulator plant of the same metal growing in the soil. In some embodiments, an increase of the pH of the soil decreases the amount of metal accumulated by the hyperaccumulator plant growing in the soil, the mobility of the one or metals released by the weatherable rock, or both. \|[0104] In some embodiments the amount of weatherable rock mixed into the soil for every hectare on which the hyperaccumulator plant is grown is optimized to maximize the growth rate of the hyperaccumulator plant. \|[0105] In some embodiments, at least 5 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, at least 10 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 10 tonnes and 100 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 5 tonnes and 10 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 25 tonnes and 50 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 35 tonnes and 40 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 100 tonnes and 200 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, about 150 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. In some embodiments, between 400 tonnes and 800 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. . In some embodiments, about 600 tonnes of weatherable rock are mixed into the soil for every hectare on which the nickel hyperaccumulator plant is grown. \|[0106] In some embodiments, at least about 20 tonnes of nickel hyperaccumulator biomass is grown per hectare. In some embodiments, at least about 400 kg, at least about 500 kg of nickel, at least about 600 kg, at least about 700 kg, at least about 800 kg, at least about 900 kg, or at least about 1,000 kg of nickel is produced per hectare. In other variations, between about 100 kg and 5000 kg, or between 250 kg and 1000 kg, or between 400 kg and 1000 kg of nickel is produced per hectare.\|[0107] In some embodiments, between about 5 tonnes and about 50 tonnes, between about 100 tonnes and about 700 tonnes, between about 500 tonnes and about 700 tonnes, between about 100 tonnes and about 600 tonnes, between about 200 tonnes and about 600 tonnes, between about 300 tonnes and about 600 tonnes, between about 400 tonnes and about 600 tonnes, between about 500 tonnes and about 600 tonnes, between about 100 tonnes and about 500 tonnes, between about 200 tonnes and about 500 tonnes, between about 300 tonnes and about 500 tonnes, between about 400 tonnes and about 500 tonnes, between about 100 tonnes and about 400 tonnes, between about 200 tonnes and about 400 tonnes, between about 300 tonnes and about 400 tonnes, between about 100 tonnes and about 300 tonnes, between about 200 tonnes and about 300 tonnes, or between about 100 tonnes and about 200 tonnes of weatherable rock are mixed into the soil for every hectare on which the hyperaccumulator plant is grown. In some embodiments, about 500 tonnes about 600 tonnes, or about 700 tonnes of weatherable rock are mixed into the soil for every hectare on which the hyperaccumulator plant is grown. \|[0108] In some embodiments, the amount of carbon dioxide sequestered is proportional to the number of Mg2+ ions liberated from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide sequestered per hectare is proportional to the number of Mg2+ ions liberated from the weathering of the weatherable rock mixed into the soil for every hectare. \|[0109] In some embodiments, the amount of carbon dioxide sequestered is proportional to the number of Ca2+ ions liberated from the weathering of the weatherable rock. In some embodiments, the amount of carbon dioxide sequestered per hectare is proportional to the number of Ca2+ ions liberated from the weathering of the weatherable rock mixed into the soil for every hectare. \|[0110] In some embodiments, the nickel hyperaccumulator plant is harvested mechanically. In some embodiments, the nickel hyperaccumulator plant is harvested manually. In some embodiments, the nickel hyperaccumulator plant is harvested by an automated process. \|[0111] In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises continuously irrigating the weatherable rock-enriched soil. In some embodiments, the plant is irrigated using a drip irrigation system. In some embodiments, the plant is irrigated using sprinkler systems. In some embodiments, growing a nickel hyperaccumulator plant in the weatherable rock-enriched soil further comprises intermittently irrigating the weatherable rock-enriched soil. In some embodiments, the plant is irrigated using a flood irrigation approach. In some embodiments, the plant is irrigated using traditional irrigation. \|[0112] In some embodiments, the pH of the weatherable rock-enriched soil is above 7. In some embodiments, the pH of the weatherable rock-enriched soil is between 7 and 14. In some embodiments, the pH of the weatherable rock-enriched soil is between 5 and 14. In some embodiments, increasing the content of the weatherable rock of the weatherable rock- enriched soil increases the pH of the soil. \|[0113] In some embodiments, ashing the harvested nickel hyperaccumulator plant comprise drying the nickel hyperaccumulator plant to provide a dried biomass composition; crushing the dried biomass composition to provide a crushed biomass composition; and burning the crushed biomass composition to provide a nickel-enriched composition. \|[0114] In some embodiments, the method further comprises quantifying the amount of carbon dioxide that is released or sequestered in one or more steps of any of the methods described herein. In some embodiments, the amount of carbon dioxide released or sequestered by a process is measured directly. In some embodiments, the amount of carbon dioxide released or sequestered by a process is measured using a proxy. In some embodiments, the quantity of Mg2+ is used as a proxy to quantify the amount of carbon dioxide sequestered by chemical weathering of the weatherable rock. \|[0115] In another aspect, provided herein is nickel metal prepared according to any of the methods described above. \|[0116] In another aspect, provided herein is a processed nickel composition comprising a substantially pure nickel, and one or more of the following: Nickel rich ashes also containing K, Ca, oxides (e.g., NiO, MgO), carbonates (e.g., K2CO3, CaCO3, K2Ca(CO3)2), K2SO4, precipitated gypsum, low-mass carboxylic acids, Ni-bearing organic and inorganic compounds. Ni-based compounds such as NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, Ni oxalate, and Ni sulfate. In some variations of the foregoing, the processed nickel composition is at least 15%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 98%, at least 99%, at least 99.8%, at least 99.9%, at least 99.99%, at least 99.999%, or at least 99.9999% pure by weight. In some embodiments, the processed nickel composition is between 15% and 100% pure by weight. \|[0117] In another aspect, provided herein is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: Nickel rich ashes also containing K, Ca, oxides (e.g., NiO, MgO) and carbonates (e.g., K2CO3, CaCCh, KiCa CCh ), K2SO4, precipitated gypsum, low-mass carboxylic acids, Ni-bearing organic and inorganic compounds. Ni-based compounds such as NiO, Ni(OH)2, nickel sulfides, nickel hydroxides, Ni oxalate, and Ni sulfate. In some embodiments, provided herein is a nickel-enriched ash comprising at least 5% nickel by weight, and one or more of the following: Ca, Fe, K, Mg, carbonates (e.g., K2CO3, CaCOs, or K2Ca(CO3 ), P, plant cells, C, H, N, O, hydroxyapatite, oxy -hydroxyapatite, or oxides (e.g., NiO, CaO, MgO, or MgNiO2). In some embodiments, the nickel-enriched ash comprises between 5% and 100% nickel by weight. \|[0118] In any of the foregoing embodiments, the weight of nickel refers to the weight of the nickel component alone, and does not include, for example, the weight of any ligands or counter ions in any complexes or salts, respectively, that the nickel is a part of. \|EXAMPLES \|[0119] The presently disclosed subject matter will be better understood by reference to the following Examples, which are provided as exemplary of the invention, and not by way of limitation. \|Example 1: Assessment of weathering rates for different soil and plant configurations\|[0120] Samples of O. decipiens (a close relative to the hyperaccumulator known in the art as O. chalcidica or A. morale) were shipped to a testing facility. There, the seeds were separated from the remainder of the plant biomass, soaked in water to prepare them for germination, and germinated. The germinated seeds were observed to have root systems. Separately, a sample of serpentinite rock was obtained, and was ground into a fine powder, herein referred to as “serpentine soil”. \|[0121] Nine sample planters were prepared, with each planter containing a specific ratio of serpentine soil to potting soil (including both pure potting soil and pure serpentine soil). Seeds of the hyperaccumulator plants were planted in eight of the nine planters, and one planter was left with no seeds, as a control. Additionally, NPK hydroponic fertilizer was added in different concentrations to the continuous, closed-loop irrigation systems of two of the planters. The experimental conditions for each planter are illustrated in FIG. 2. \|[0122] Because Mg2+ is released in the weathering reaction of serpentine, the quantity of Mg2+ leached from the soils in each planter was used as a proxy for the rate of weathering that occurred under each condition. Over the course of 4 months, the total concentration of Mg2+ leached into the closed-loop irrigation system was measured for each of the nine planter conditions shown in FIG. 2. The results of these measurements are shown in FIG. 3. Surprisingly, it was found that quantity of Mg2+ leached by the soil mixtures increased over time as the plants grew. Further, the rate of weathering, as assessed using Mg2+ leaching as a proxy, was found to correlate to plant biomass growth. \|Example 2: Field-scale enhanced rock weathering experiment \|[0123] A field-scale trial was employed to investigate the synergistic combination of nickel phytomining and enhanced weathering. The principal aim of this experiment was to evaluate the scope for nickel extraction by the hyperaccumulator plant Odontarrhena decipiens and to quantify the carbon capture potential of crushed serpentinite rock added to the naturally occurring serpentine agricultural soil. \|[0124] A 112 m x 168 m field site was selected for this trial based on aerial photography and ground observations. Four permanent reference points for determining precise locations were established by cementing steel posts into the ground at the comers of the field site. The area was then partitioned into four equally-sized rectangular blocks, each measuring 56 m x 84 m. A scale diagram of the randomized complete block design used in the trial is shown in FIG. 4. These blocks represent replicates, such that each block contained eight randomized 12 m x 18 m plots (one for each of the eight rock treatments) separated by an 8 m margin of untreated land. The amount of rock treatment added to each plot as measured in tonnes of serpentinite rock per hectare is shown in FIG. 4. The randomized complete block design accounts for the effects of extraneous variables (e.g. hydrological gradients across the site) and hence, mitigates bias caused by inherent variation. \|[0125] The entire field site was tilled prior to the trial. Crushed serpentinite rock was sourced from a nearby quarry and applied by hand to the soil surface of each plot at rates ranging from 9.375 to 600 tonnes per hectare, whereby the next higher rate was set to be double the previous as illustrated in FIG. 4. Each block also contains a ‘control’ treatment where no serpentinite rock is added (i.e. 0 tonnes per hectare), against which all other treatments were compared statistically. The applied rock material was incorporated into the soil to an approximate depth of 150 mm using a rotavator. One-year-old Odontarrhena decipiens specimens were then transplanted into each plot, in thirteen rows with 1 m rowspacing and 0.5 m spacing between the individual plants. Organic fertilizers, pesticides, and fungicides were added to the experimental plots to ensure baseline crop performance and mitigate pest/pathogen interference in all treatments. \|[0126] At the beginning of the experiment, over a hundred mesh bags were filled with 0.4 g of crushed serpentinite and buried in the plots at soil depths between 50-200 mm. Retrieval of the grains from these bags at the end of the trial permits the direct assessment of mineral weathering through X-ray analysis. \|Soil sample collection and measurements \|[0127] Before applying the serpentinite rock material, fifteen baseline soil samples were collected from each block using a steel auger and following a W-shaped sampling pattern. These initial (pre-planting, pre-rock application) soil samples are taken from three depths: 0- 0.3 m, 0.3-0.6 m, and 0.6-0.9 m. Soils are then passed through a 2 mm mesh size sieve, air dried, and tested for the following physical and chemical parameters: pH (in H2O and IM KC1); organic matter and humus %; plant-available nitrogen, phosphorus and potassium; soil texture (sand/silt/clay %); cation exchange capacity; and, total and plant-available Ca, Mg, K, Na, Fe, Cd, Co, Cr, Cu, Mn, Ni, Pb, and Zn. Further soil samples were collected monthly from each of the thirty-two experimental plots and tested for pH, electrical conductivity, cation exchange capacity, and plant-available cations. These data were used to monitor changes in the concentrations of plant-available nutrients and nickel over time, and to estimate rock weathering and carbon dioxide capture rates via a conventional mass balance approach, in combination with novel quantification methods. \|Plant sample collection and measurements \|[0128] Aboveground plant tissues are harvested from all plots after a suitable time (e.g., approximately 6-8 months) after the trial began. Plant materials are dried and weighed to determine crop yields, and ground for analysis of nutrients and metals. These data are used to measure the efficiency of nickel uptake by the hyperaccumulator plants, and to evaluate the correlation between rock application and nickel uptake rates. Moreover, values for total uptake of calcium, magnesium, potassium and sodium are fed into mass budget calculations for carbon capture quantification. \|[0129] Aboveground plant tissues were harvested from five different mature hyperaccumulator plant specimens randomly selected from all plots after a suitable time (e.g., approximately 6-8 months) after the trial began. Plant samples were washed with distilled water, dried in a forced-air oven at 60 °C for 48 hours, and powdered separately using a laboratory grinding mill. These plant samples were used to determine total heavy metal concentrations in the plant tissues. \|Soil pH and electrical conductivity measurements \|[0130] The pH and the electrical conductivity (EC) of the soil samples determined using a Combined Conductivity /pH Meter equipped with a temperature input, which internally corrects for the effect of temperature on measured values. pH and EC were standardized using a 3-point calibration protocol with certified reference solutions (buffers at pH 4.00, 7.00, and 14.00; EC standards at 12.88 mS, 1413 pS, and 84 pS). To streamline the measurements, pH and EC were tested sequentially from the same sample. For each soil sample, 15.0000 ± 0.0005 g of soil was weighed into a 50 mL polypropylene centrifuge tube and combined with 30.0000 ± 0.0150 mL of ultrapure water (resistivity of 18.2 MQ-cm at 25 °C). The tubes were stoppered, agitated on a rotary shaker for 3 minutes, unstoppered and then left to equilibrate with the atmosphere for 30 minutes. An additional three replicates of control soil (initial/baseline soil containing no additives) were prepared and used to precondition the pH and conductivity electrodes prior to analysis of the experimental samples. This preconditioning process shortens the timescales for stable measurements and mitigates measurement error in the first few experimental samples (e.g. due to contamination with trace amounts of buffer solution). To obtain pH measurements, the pH electrode was swirled into the soil-water mixture’s supernatant for 10 seconds, and then gently released into the slurry until the instrument identified that a stable pH reading was achieved (or 3 minutes after initial insertion, where stabilization was not achieved). pH measurements were recorded to 0.001 pH units, and the electrode was rinsed thoroughly with ultrapure water between samples. To obtain EC measurements, the conductivity electrode was inserted into the soilwater mixture’s supernatant and held until the instrument indicated that a stable EC reading was achieved (or 1 minute after initial insertion, where stabilization was not achieved). EC measurements were recorded to four significant figures, and the electrode was rinsed thoroughly with ultrapure water between samples. \|Soil analysis methods for total heavy metals \|[0131] The soil samples were tested for total heavy metals by first drying a test portion of the soil and reducing the grain size of the soil to below a particle size of 250 microns. Each test portion of the soil was then weighed (0.5 g to 1.0 g based on dry mass) and transferred to a microwave extraction vessel. A few drops of water were then added to the extraction vessel before adding a HC1 and nitric acid solution and mixing well. The temperature of the extraction mixture was increased at a rate of approximately 10 °C/min to 175 ± 5 °C using a microwave digestion system. The amount of total Ni in the soil samples was then determined using ICP-OES. \|Availability ofNi with Mehlich-1 digestion \|[0132] The soil samples were prepared by mixing 5 g of the soil samples with 20 mL of a Mehlich-1 extraction solution consisting of a mixture of HC1 and H2SO4. The mixture was then stirred for 5 min at 180 cycles/min after which the suspension was allowed to rest for 16 h before decanting off the supernatant The total amount of Ni in the soil samples was then determined by testing an aliquot of the supernatant using ICP-OES. \|Other analytical methods \|[0133] It should be understood that one or more additional techniques may be used to determine the amount of Ni in the soil, the amount of rock-derivable cations in the tissue of the hyperaccumulator plants or the soil, the amount of heavy metals in the tissue of the hyperaccumulator plants or the soi, the pH of the soil, the electrical conductivity of the soil, and other aspects of the weatherable rock, soil, and hyperaccumulator plants, including quantification of the weathering rate. For example, X-ray fluorescence analysis of weathered rock material (retrieved from mesh bags buried in the plots) is used to quantify changes in grain surface chemistry. These data provide an independent method for mineral weathering rate quantification. The loss of cations from the added rocks may serve as a proxy for the accumulation of cations released from this process in the plant and soil. \|Determination of total heavy metal and Ca, Mg, K concentrations in plants with digestion\|[0134] Aboveground plant tissues were digested in an acid solution (HNO3 65% and H2O2 30%) using a microwave digestion system to determine total heavy metal concentrations in plants. A sample of the plant matter (300 mg) was mixed with 2 mL of HNO3 and 2 mL of H2O2, stirred for at least 20 min, and then digested using a microwave digestion system. Plant tissue samples calibration curves were plotted from Ni concentrations of 2, 4 and 6 mg/L. The solution was diluted 20 times. The amount of Ni in the plant tissue samples was then determined using ICP-OES. \|Results and Analysis \|[0135] Approximately 8 months after the trial began, representative soil samples were collected from the plots for analysis. As shown in FIG. 5, increasing serpentinite application rates resulted in increasing soil pH. Moreover, application rates above 0.9375 kg m 2 resulted in statistically significant increases in soil pH with respect to the control soils, where no serpentinite rocks were added, which is evidence of chemical weathering of the added serpentinite rock. Surprisingly, soil pH continued to increase with increasing application rates, and rose substantially to the highest recorded level at the highest application rate (60 kg m 2) as shown in FIG. 5. Chemical weathering of the added alkaline minerals (e.g. serpentinite rock) will lead to carbon dioxide sequestration. Enhanced weathering of the added rock material is also supported by evidence of elevated soil electrical conductivity (EC) following rock applications as shown in FIG. 6. Higher EC indicates the release of cations due to rock dissolution, and similarly represents evidence for chemical weathering of the serpentinite rock applied to the soil. This chemical weathering leads to carbon dioxide sequestration. \|[0136] Amendment of soils with serpentinite rock also resulted in higher nickel uptake into the tissues of the hyperaccumulator plants as compared to the hyperaccumulator plants grown in the control soils, with the highest nickel yields observed in soils amended with 3.75 to 15 kg m 2 of serpentinite rock as shown in FIG. 7. The mean total Ni yield from the hyperaccumulator plants was calculated by multiplying the (dry) biomass yield by the (dry) biomass Ni concentration. Mean total Ni yields from the hyperaccumulator plants ranged from around 1.4 g Ni m 2 (14 kg Ni ha 1) in the control plots to a peak of about 2.5 g Ni m 2 (25 kg Ni ha 1) in the plots treated with 15 kg m 2 (150 t ha 1) of serpentinite rock. Plants grown on soils with elevated pH will typically accumulate less nickel. Surprisingly, nickel yields increased in the soils amended with 3.75 to 15 kg m 2 of serpentinite rock, which implies that the combination of enhanced weathering of serpentinite and nickel hyperaccumulators realized a synergistic benefit. Overall, this data indicates mass transfer of Ni from the applied serpentinite rock into the tissues of the hyperaccumulator plants. \|[0137] Timeseries data for soil-extractable Ni was determined by a Mehlich 1 extraction procedure and confirms that soil concentrations increased in all plots treated with serpentinite rock between when the trial began (0 m) and the following spring (~5 m), when the hyperaccumulators would have exhibited low primary production as shown in FIG. 8. However, the subsequent steep reduction in soil Ni concentrations between spring (~ 5 m) and mid-summer (~7 m) is evidence for the uptake of soil Ni and depletion of the soil Ni pool by the hyperaccumulator plants at a time of increasing primary productivity as shown in FIG. 8. This data is evidence of the synergy between the two processes because depletion of the soil nickel pool by hyperaccumulator plants can be offset through the weathering of additional nickel bearing-minerals (e.g., serpentinite) introduced to the soil, resulting in carbon negative nickel recovery. \|Statistical analyses \|[0138] Statistical analysis was also performed to determine the significance of the relationships between rock application, plant nickel uptake, and (potential) carbon capture rates. Statistical analysis of the soil data was performed using a linear mixed model with fixed model Treatment * Time and random model of Block/Plot. Where appropriate, variables were first transformed to ensure homogeneity of variance. F statistics were obtained using the Kenward-Roger approximation. Statistical analysis of the plant data was performed using a linear model accounting for differences between blocks. A third order polynomial was fitted over application rate with highest order terms successively dropped if found to be non- significant. \|[0139] Regarding soil pH, statistically significant differences were observed both between treatments (F4, 12=21.54, p < 0.0001) and over time (F3, 45=7.18, p=0.0005). Predicted means and standard errors for each significant main effect is shown in FIGS. 9 and 10. For Soil EC, statistically significant differences were observed both between treatments (F4, 12=3.28, p = 0.049 - a marginal effect) and over time (F3, 45=8.59, p=0.0001). Predicted means and standard errors for each significant main effect are shown FIGS. 11 and 12. For ammonium acetate (AA) extractable nickel, statistically significant differences were observed both between treatments (F4, 12=5.66, p = 0.008) and over time (F3, 45=10.03, p<0.0001). Predicted means and standard errors for each significant main effect is shown in FIGS. 13 and 14. For ammonium acetate extractable magnesium, a statistically significant interaction effect was found between treatment and sampling date (F12,45=2.27, p=0.02). Overall, the largest effect is attributed to differences over time (F3, 45=6.81, p=0.007). Predicted means and standard errors are shown in FIG. 15. A multivariate correlation figures between all soil data can be seen in FIG. 16. \|[0140] The above preliminary data was collected over the first 8 months of the field trial experiment. Additional data will be gathered until 12 months after the start of the field trial experiment to further elucidate the relationship between the application rate of the weatherable rock and the accumulation of metal by the hyperaccumulator plant, the soil pH, the soil electrical conductivity, the weatherable rock-derivable cations in the soils and plants, and the heavy metals in the soils and the plants, as well as determining the weathering rate of the weatherable rock, the amount of nickel ore extractable from the plants, and quantifying the amount of carbon dioxide sequestered. \|Example 3: Field-scale enhanced rock weathering experiment with two controls\|[0141] In this example, a field- scale trial is employed to further investigate the synergistic combination of nickel phytomining and enhanced weathering. A scale diagram of the randomized complete block design used in the trial is shown in FIG. 17. The trial uses an approximately level 112 m x 208 m field site that is divided into four blocks of equivalent area, each measuring 56 m x 104 m, with every block subdivided into 10 randomly-assigned 12 m x 18 m plots representing the ten treatments as shown in FIG. 17. The amount of rock treatment added to each plot as measured in tonnes of serpentinite rock per hectare is shown in FIG. 17. Neither rock nor hyper- accumulator plants are added to the plots marked with ‘XX’ in FIG. 17. These plots are designed to simulate native soil conditions. The plots are segregated by an 8 m margin of untreated land. \|[0142] Two control treatments are included in this study: a rock-free control (i.e. 0 tonnes of rock added per hectare) where hyperaccumulator plants are grown, and a second control where no plants, rock amendments, or management practices are employed, as denoted by ‘XX’ in FIG. 5. The rock-free control is used to assess the effect of different rock applications on nickel uptake efficiency and carbon capture. The experiments with no plants, rock amendments, or management practices control serves a baseline (the native soil’s background conditions). \|Soil sample collection and measurements \|[0143] Following a W-shaped sampling pattern, multiple baseline soil samples are collected and aggregated from each of the forty plots at three discrete depths (0-0.3, 0.3-0.6 and 0.6-0.9 m) using a steel auger. These initial soil samples are separately homogenized, passed through a 2-mm mesh size sieve, and air-dried. Soils are then tested for pH (in H2O and IM KC1) and electrical conductivity (in H2O); inorganic/organic carbon and nitrogen %; plant-available nitrogen, phosphorus and potassium; soil texture (sand/silt/clay %), bulk density and water holding capacity; cation exchange capacity and exchangeable acidity; major oxide and soil mineralogy %; and, total and plant-available Ca, Mg, K, Na, Fe, Cd, Co, Cr, Cu, Mn, Ni, Pb, and Zn. Further soil samples are taken at bi -monthly intervals and tested to determine changes in fundamental soil parameters (pH, electrical conductivity, organic/inorganic carbon) and the concentration of exchangeable (plant- available) metals. These data are critical for monitoring changes in nickel availability and carbon dioxide capture rates in the plots. \|Plant sample collection and measurements \|[0144] Approximately 1-year after the start of the field trial, shoot tissues are harvested from all plots, and the shoot tissues are dried and weighed to quantify crop performance. In addition, plant materials are powdered, digested, and tested to determine metal content and analyze the correlation between rock application rate and nickel uptake efficiency. Total plant calcium, magnesium, potassium, and sodium values are added to the respective values from the soil analyses of exchangeable elements, which together enable the quantification of rock weathering and carbon capture rates. \|Aqueous sample collection and measurements \|[0145] Pore water samples are extracted from the soil using lysimeters installed in the plots. These aqueous samples are analyzed for changes in the following parameters: pH, electrical conductivity, and alkalinity; and dissolved cations (e.g. nickel, magnesium) and anions (e.g. chloride, nitrate). These data are essential for accurate monitoring of rock dissolution, nickel release, and carbon capture rates. Soil-atmosphere greenhouse gas sample collection and measurements \|[0146] Gaseous samples are collected during the trial using static chambers installed in the plots and are analyzed using gas analysis mass spectrometry to determine soil-atmosphere fluxes of major greenhouse gasses, such as carbon dioxide, methane, and nitrous oxide. This example seeks to determine the effects of the addition of alkaline rocks to the soil on overall emissions of potent non-CCh greenhouse gasses, and thus impact on climate change. These gas measurements are performed in serpentine soils, and also provide evidence that the soil amendments and agricultural management practices associated with the trial result in the conversion of existing soil organic carbon into atmospheric carbon dioxide. \|Example 4: Life Cycle Assessment at Kilotonne and Megatonne Scales Per Year\|[0147] A Life Cycle Assessment (LCA) was employed to ensure that the enhanced rock weathering/hyperaccumulator plant operation is sufficiently CO2 negative at the necessary scale. The aim was to model the net sequestration of 1 kilotonne and 1 megatonne of CO2 per year. The LCA was conducted using SimaPro software which draws data from various databases. The study adopted a cradle-to-gate approach, which includes all the major processes in the life cycle from the mining operation to the production of nickel ore, however the environmental impact of waste treatment was excluded from the LCA due to the ambiguity of its relevance. The two products of the operation are CO2 uptake (carbon dioxide removal through enhanced rock weathering) and the production of nickel ore through phytomining. The major processes within the established system boundaries include the mining, crushing, and milling of serpentine, the transportation of the serpentine rock to the site of placement, the fertilizer used, and harvesting, drying, and combustion of the hyperaccumulator plants. A unit area of land was used as the functional unit for the LCA to account for both the CO2 extraction and the nickel ore production. For example, per every m2 of area of serpentine soil used for the cultivation of A. Murale (or a similar hyperaccumulator plant), a certain amount of nickel will be produced and a certain amount of CO2 will be sequestered. This functional unit ensures that neither of the two products of the system (i.e. CO2 uptake and the production of nickel ore) are neglected from the LCA analysis and that their amounts are calculated independently of each other. \|[0148] The data used for the LCA was collected from several sources and the model was built on the basis of existing models. The data related to standard transportation, machinery, energy, and materials were kept as they were in the models, apart from several necessary adjustments to bring the model closer in line with the operation. For example, during the whole process, the electricity comes from the grid, where it is mostly produced using hydropower. This feature was reflected in the model. It is not required that hydropower be utilized in the process, though it will lower the net negative efficiency. A range of parameters, such as the weathering rate and serpentine content in soil, was introduced into the model. The information used to determine the parameter values was sourced from a combination of existing literature on similar experiments with hyperaccumulators and mineral weathering. The firm relied on rates of natural weathering processes which resulted in calculations that predict significant CO2 uptake and nickel production. \|[0149] The models for 1 kilotonne-scale production yearly can be seen in FIG. 18. The 1 megatonne-scale chart can be seen in FIGS. 19A and 19B. The main difference between the operations is the increased transport distance between the serpentine mining site and the farming sites in the megatonne- scale model as compared to thel kilotonne-scale model. Although not incorporated into the model, utilizing renewable energy for transportation of the rock between the mining site and farming sites would help ensure that the process remains CO2 negative even with long transportation distances. According to this LCA study, the operation can run at scale at an approximately 90% net efficiency in terms CO2 sequestration; additional details of the LCA study can be found in FIG. 20.	Family Number\|(108265090)\|108265090\|Object of Invention\|(WO202420548 A2)\| (...) particles to increase reactive mineral surface area, dispersing the weatherable rock particles into the soil within a plot of land, planting nickel hyperaccumulating plants onto the plot of land to capture the nickel released from the weatherable rock during chemical weathering.\|Abstract\|(ID202507231 A)\|Methods are provided for extracting metals from rocks and sequestering (capturing and storing) carbon dioxide. In some embodiments, methods are provided to use phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. Compositions are also provided, which include metal compositions made by the methods here. Provided are methods of extracting metals from rocks and sequestering carbon dioxide. In some embodiments, provided are methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. Provided are also compositions, including metal compositions produced by the methods herein.\|Independent Claims\|(WO202420548 A2)\| (...) weatherable rock to undergo a chemical weathering process at an accelerated rate relative to natural chemical weathering, wherein the chemical weathering process generates alkalinity and releases the metal, and wherein the alkalinity facilitates the sequestration of carbon dioxide by converting carbon dioxide to bicarbonate or carbonate; and extracting and processing the released metal to provide a metal-enriched composition.\|	Chemical engineering\|Environmental technology\|Materials, metallurgy	C22B-001/00\|C22B-001/14\|C22B-003/08\|C22B-003/26\|C22B-003/42\|C22B-003/44\|C22B-023/043\|C22B-023/0453\|C22B-023/0461\|C22B-026/22\|C25C-001/08\|Y02C-020/40		C22B-001/00\|C22B-001/14\|C22B-003/08\|C22B-003/26\|C22B-003/42\|C22B-003/44\|C22B-023/043\|C22B-023/0453\|C22B-023/0461\|C22B-026/22\|C25C-001/08\|Y02C-020/40	B01J-047/02\|B09C-001/00\|C01G-053/00\|C22B-003/00\|C22B-003/04\|C22B-003/08\|C22B-003/18\|C22B-003/44\|C22B-007/00\|C22B-023/00	B01J-047/02\|B09C-001/00\|C01G-053/00\|C22B-003/00\|C22B-003/04\|C22B-003/08\|C22B-003/18\|C22B-003/44\|C22B-007/00\|C22B-023/00					US6159270\|US6786948	US6159270 60049318 WHO=Examiner SELF=N CAT=A\|US6786948 1414600 WHO=Examiner SELF=N CAT=A		XP093159640; XP087050049; XP093159650; XP093159654; US6159270; US6786948\|\|\|	\|(WO2024/020548)\|International Search Report [Examiner]\|-CRISTINA BECERRA-CASTRO: "Bacterially Induced Weathering of Ultramafic Rock and Its Implications for Phytoextraction", APPLIED AND ENVIRONMENTAL MICROBIOLOGY, AMERICAN SOCIETY FOR MICROBIOLOGY, US, vol. 79, no. 17, 1 September 2013 (2013-09-01), US , pages 5094 - 5103, XP093159640, ISSN: 0099-2240, DOI: 10.1128/AEM.00402-13\|-JALLY BASTIEN; FRANÇOIS MATHILDE; KESSLER MORGANE; LAUBIE BAPTISTE; SIMONNOT MARIE-ODILE: "Recovery of nickel from strongly acidic bio-ore leachate using a bispicolylamine-based chelating resin", SEPARATION AND PURIFICATION TECHNOLOGY, ELSEVIER SCIENCE, AMSTERDAM, NL, vol. 293, 20 April 2022 (2022-04-20), NL , XP087050049, ISSN: 1383-5866, DOI: 10.1016/j.seppur.2022.121126\|-TIMOTHY LENTON: "First plants cooled the Ordovician", NATURE GEOSCIENCE, no. 5, 1 February 2012 (2012-02-01), pages 86 - 89, XP093159650, DOI: 10.1038/ngeo1390\|-PETRA SUSAN KIDD: "Developing Sustainable Agromining Systems in Agricultural Ultramafic Soils for Nickel Recovery", FRONTIERS IN ENVIRONMENTAL SCIENCE, FRONTIERS MEDIA, vol. 6, XP093159654, ISSN: 2296-665X, DOI: 10.3389/fenvs.2018.00044\|\|\|	PENDING	(EP4558651)\|PENDING\|(WO2024/020548)\|LAPSED\|(ID2025/07231)\|PENDING\|(TW202417649)\|PENDING	ALIVE	(EP4558651)\|ALIVE\|(WO2024/020548)\|DEAD\|(ID2025/07231)\|ALIVE\|(TW202417649)\|ALIVE	(EP4558651)\|LEGAL DETAILS FOR EP4558651\|Actual or expected expiration date=2043-07-21\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-07-21\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP23843926\|Application date=2023-07-21\|Standardized application number=2023EP-0843926\|Event publication date=2024-01-26\|Event code=EP/STAAPCT\|Event group=Examination events Entry into national phase\|The international publication has been made\|Original code: STAA\|Event publication date=2025-04-25\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN 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expiration date=2043-07-21\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-07-21\|Event code=TW/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=TW TW112127364\|Application date=2023-07-21\|Standardized application number=2023TW-0127364\|Event publication date=2024-05-01\|Event code=TW/A\|Event indicator=Pos\|Event group=Examination events\|Laid open application for patent or patent of addition\|Publication country=TW\|Publication number=TW202417649\|Publication stage code=A\|Publication date=2024-05-01\|Standardized publication number=TW202417649	(EP4558651)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4558651)\|Extension States: BA\|(EP4558651)\|Validation States: MA, MD, TN, KH\|(WO2024/020548)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2024/020548)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2024/020548)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2024/020548)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2024/020548)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP4558651)\|EP\|(WO2024/020548)\|EP; ID\|(ID2025/07231)\|ID\|(TW202417649)\|TW	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=nwH/nfofj4/DzwgmQHVFUW8tmrmn8uQzNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006462121&ekey=2357&xpn=EP4558651&kind=A2	https://register.epo.org/application?number=EP23843926	https://permalink.orbit.com/RenderStaticFirstPage?XPN=0hvHXPoHlmIuw56Xk6cpNXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2024/020548)\|US\|(WO2024/020548)\|US\|(TW202417649)\|US	(WO2024/020548)\|NAME=METALPLANT PUBLIC BENEFIT CORPORATION 2810 N Church St PMB 88709 Wilmington, Delaware 19802-4447 , COUNTRY=US\|(WO2024/020548)\|NAME=METALPLANT PUBLIC BENEFIT CORPORATION 2810 N Church St PMB 88709 Wilmington, Delaware 19802-4447 , COUNTRY=US\|(TW202417649)\|NAME=METALPLANT PUBLIC BENEFIT CORPORATION , COUNTRY=US	(EP4558651)\|GB\|(WO2024/020548)\|US\|(WO2024/020548)\|US\|\|	(EP4558651)\|NAME=J A Kemp LLP 80 Turnmill Street , CITY=London EC1M 5QU , COUNTRY=GB , REG=101669666\|(WO2024/020548)\|NAME=ROBERTS, Emily Jane et al. Morrison & Foerster LLP 425 Market Street San Francisco, California 94105 , POSTCODE=94105 , COUNTRY=US\|(WO2024/020548)\|NAME=ROBERTS, Emily Jane et al. Morrison & Foerster LLP 425 Market Street San Francisco, California 94105 , POSTCODE=94105 , COUNTRY=US\|(ID2025/07231)\|NAME=Marolita Setiati\|(TW202417649)\|NAME=CHEN, CHANG-WEN NAME=CHANG, CHE LUN NAME=LO, WEN-MIAO	(EP4558651)\|US; US\|(WO2024/020548)\|US; US\|(WO2024/020548)\|US; US\|\|(TW202417649)\|US; US	(EP4558651)\|NAME=MATZNER, Eric Jason, CITY=Wilmington, Delaware 19802-4447, COUNTRY=US \|NAME=WASSERSON, Laura R., CITY=Wilmington, Delaware 19802-4447, COUNTRY=US\|(WO2024/020548)\|NAME=MATZNER, Eric Jason c/o MetalPlant Public Benefit Corporation 2810 N Church St, PMB 88709 Wilmington, Delaware 19802-4447, POSTCODE=19802-4447, COUNTRY=US \|NAME=WASSERSON, Laura R. c/o MetalPlant Public Benefit Corporation 2810 N Church St, PMB 88709 Wilmington, Delaware 19802-4447, POSTCODE=19802-4447, COUNTRY=US\|(WO2024/020548)\|NAME=MATZNER, Eric Jason c/o MetalPlant Public Benefit Corporation 2810 N Church St, PMB 88709 Wilmington, Delaware 19802-4447, POSTCODE=19802-4447, COUNTRY=US \|NAME=WASSERSON, Laura R. c/o MetalPlant Public Benefit Corporation 2810 N Church St, PMB 88709 Wilmington, Delaware 19802-4447, POSTCODE=19802-4447, COUNTRY=US\|(ID2025/07231)\|NAME=MATZNER Eric Jason\|NAME=WASSERSON Laura R\|(TW202417649)\|NAME=MATZNER ERIC JASON, COUNTRY=US \|NAME=WASSERSON LAURA R, COUNTRY=US		3	4			(EP4558651)\|WO2024/020548\|(ID2025/07231)\|WO2024/020548		(WO2024/020548)\|Number of Claims: NCL=1\|\|(WO2024/020548)\|Number of Claims: NCL=28\|Extended kind: EXTK=z\|\|(TW202417649)\|Number of Claims: NCL=28\|		(EP4558651)\|ENGLISH (ENG)	(ID202507231)\|Patent\|(EP4558651)\|Patent\|(TW202417649)\|Patent\|(WO202420548)\|Patent\|(WO202420548)\|Patent	Titre: (EP4558651)\|Methods for obtaining carbon neutral or carbon negative metals from plants, and related compositions Résumé: (EP4558651)\|Provided are methods of extracting metals from rocks and sequestering carbon dioxide. In some embodiments, provided are methods of using phytomining to extract metals from ultramafic rocks while sequestering carbon dioxide. Provided are also compositions, including metal compositions produced by the methods herein.	34	Abstract	gpt-4o-mini	uncertain	The article mentions sequestering carbon dioxide in the context of extracting metals from ultramafic rocks, but it does not explicitly focus on accelerated weathering or the specific processes related to mineral carbonation.
35	CN201510055353	CN201510055353	CN104696005\|CN104696005	69557757	CN104696005 B 2016-08-31 [CN104696005B]\|CN104696005 A 2015-06-10 [CN104696005]	2015-02-03	2015-02-03	2016-08-31\|2015-06-10	(CN104696005B)\|2016-08-31	(CN104696005)\|2035-02-03	(CN104696005)\|Method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in old goaf of coal mine	(CN104696005)\|The invention discloses a method for synchronously extracting residual coalbed methane and sealing and preserving carbon dioxide in an old coal mined-out area of coal mine. The method comprises the following steps: during working face mining, a pipeline is paved at the bottom of a mining roadway, seam grooves are axially formed in the pipeline at intervals, baffles are arranged on both ends of each seam groove, high-pressure hoses are respectively wound on the seam grooves, water under a certain pressure is injected in the high-pressure hoses to perform 'yielding' protection on the pipeline, so that crushed coal and rock in the mined-out area can be prevented from destroying the pipeline and blocking air holes; after working face mining is finished, a fire dam is arranged at a mining stop line, the pipeline is communicated to the ground, and well drilling is constructed from the ground to the upper part of the mined-out area; CO2 is injected from the ground to the mined out area along the pipeline, because the density of the CO2 is larger than CH4, and the crushed coal and rock remained at the bottom of the mined-out area has higher adsorptivity to CO2, the absorbed CH4 is replaced out and is accumulated at the top of the mined-out area, and the accumulated CH4 is extracted by well drilling. The method has dual benefits of sealing and preserving the carbon dioxide, and developing and utilizing the residual coalbed methane.	TAIYUAN UNIVERSITY OF TECHNOLOGY	(CN104696005)\|TAIYUAN UNIVERSITY OF TECHNOLOGY ([CN])\|(CN104696005)\|TAIYUAN UNIVERSITY OF TECHNOLOGY	HU SHENGYONG\|GAO QIANG\|CHEN CHUNJIAN\|ZHANG XIANG	(CN104696005)\|HU SHENGYONG\|GAO QIANG\|CHEN CHUNJIAN\|ZHANG XIANG\|(CN104696005)\|HU SHENGYONG\|GAO QIANG\|CHEN CHUNJIAN\|ZHANG XIANG	(CN104696005)\|LU MAOCHUN;KERUIDA PATENT AGENCY CO., LTD. TAIYUAN CITY\|Reg. Nb: 14101		(CN104696005)\|1. The method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in the old goaf of the coal mine is characterized by comprising the following steps:a. in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) from a position 5-10 m away from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5);b. tightly winding a high-pressure hose (7) with the diameter of 5-15 cm and the compressive strength of 5-10 MPa on the slot (5), injecting 2-5 MPa high-pressure water into the high-pressure hose (7) when all pipelines (4) wound with the high-pressure hose (7) enter a goaf (8), and bundling a water injection port of the high-pressure hose (7) after water injection is finished;c. after the stoping of the working face (1) is finished, a closed wall (10) with the thickness of 2-5 m is arranged at the stoping line (9), and the pipeline (4) penetrates through the closed wall (10) and is connected to the ground (11) and the CO2A gas storage tank (12) is communicated with CO2A first valve (13) is arranged at an air outlet of the air storage tank (12);d. constructing a well (14) downwards from the ground (11) every 200-300 m along the middle of the goaf (8) until the bottom of the well (14) is 20-40 m away from the upper part of the goaf (8), inserting an extraction pipe (16) into the well (14) from the ground (11), and arranging a second valve (17) at the upper end of the extraction pipe (16);after the well mouth of the drilling well (14) is sealed, an extraction pipe (16) is connected with a pump station (15);e. opening a first valve (13) by CO2The gas storage tank (12) injects CO into the goaf (8) along the pipeline (4)2Simultaneously opening a second valve (17) to begin extracting CO in the goaf (8)2Displacing residual coal bed gas;f. when extracting CO in the pipe (16)2When the concentration is higher than 10%, the first valve (13) and the second valve (17) are closed, and the CO injection is stopped2And extracting residual coal bed gas.\|	(CN104696005)\|The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction, which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf.\|the invention discloses a method for cooperatively sealing carbon dioxide and developing residual coalbed methane in a coal mine goaf, which comprises the following steps: in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) at a distance of 5-10 m from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5).\|	(CN104696005)\|COALBED GAS(100,12)\|OLD GOAF(100,10)\|COAL MINE(100,8)\|COAL MINE OLD GOAF(100,6)\|EXTRACTING RESIDUAL COALBED GAS(100,6)\|RESIDUAL EXTRACTION(100,6)\|SEALING(100,4)\|METHANEDIONE(100,3)\|METHANEDIONE COOPERATIVE SEQUESTRATION(100,1)\|STOPING ROADWAY(84,4)\|METHANEDIONE SEQUESTRATION(73,3)\|RESIDUAL COALBED METHANE(66,4)\|PIPELINE(60,23)\|SEQUESTERING CO OPERATIVE(58,1)\|RESIDUAL COALBED METHANE DEVELOPMENT(57,1)\|GOAF(53,22)\|RESIDUAL COALBED METHANE EXTRACTION(53,2)\|GOAF MIDDLE(52,1)\|METHANEDIONE SEQUESTRATION DOUBLE BENEFIT(51,1)\|EXTRACTION PIPE(46,10)\|ADSORBED CH4AND(46,1)\|WORKING FACE STOPING(43,4)\|WORKING FACE(39,6)\|CH4AND BROKEN COAL(38,1)\|METHANE EXTRACTION(37,1)\|SLIT GROOVE(35,2)\|BAFFLE(33,3)\|SEALING METHANEDIONE(33,2)\|CUTTING HOLE(31,3)\|RESIDUAL COALBED GAS(29,3)\|STOPING(26,4)\|BROKEN COAL ROCK(25,3)\|WORKING FACE STOPING(25,2)\|CO2A GAS STORAGE TANK(25,1)\|RESIDUAL COALBED GAS UTILIZATION(25,1)\|PIPE WALL(24,3)\|CLOSURE WALL(22,2)\|PIPELINE2DUE(22,1)\|DUAL BENEFIT(19,1)\|EXTRACTING(18,2)\|CO2THE GAS STORAGE TANK(17,4)\|STOPING LINE(17,4)\|GAS STORAGE TANK(13,7)\|NONPRODUCTIVE COAL SEAMS2OUTSTANDING(13,1)\|COMPRESSIVE STRENGTH(12,3)\|WATER INJECTION(10,5)\|PUMP STATION(10,4)\|METHANEDIONE SEQUESTRATION BENEFIT(10,1)\|SEALING WALL(9,6)\|WELL DRILLING(9,6)\|AIR STORAGE TANK(9,3)\|RESIDUAL COALBED METHANE RESOURCE(9,1)\|AIR OUTLET(8,2)\|CO2HAS STRONG ADSORBABILITY(8,1)\|COAL PILLAR CRACK(8,1)\|ADSORBED CH4IS(7,1)\|CH4THE PROMINENCE(7,1)\|CO2DENSITY OFGREATER(7,1)\|CO2FOR DISASTER(6,1)\|COAL SEAM STORE CO2CO(6,1)\|GEOLOGICAL DISPOSAL(6,1)\|MINE ROADWAY(6,1)\|VENTILATION BURDEN(6,1)\|IGNITION PHENOMENON NATURE(5,1)\|INTRODUCING CO2SEALING(5,1)\|RELEVANT SCIENTIST(5,1)\|ABANDONED RESIDUAL(4,1)\|COAL MINING RAPID DEVELOPMENT(4,1)\|COAL RESIDUE(4,1)\|DISPLACING RESIDUAL COALBED GAS(4,1)\|GLOBAL CONCERN(4,1)\|RESIDUAL DISPLACEMENT(4,1)\|STORE CO2IT(4,1)\|ADSORPTIVITY(3,1)\|ATMOSPHERE2THE(3,1)\|DUCT SLOT(3,1)\|GOAF4THE GAS EXTRACTION(3,1)\|LIVING ENVIRONMENT(3,1)\|PIPE PROTECTION(3,1)\|SIGNIFICANCE(3,1)\|UNSAFE FACTOR(3,1)\|ADDITIVE(2,1)\|COAL ROCK MASS PAIR(2,1)\|COALBED GAS INDUSTRY(2,1)\|FACE EXTRACTION(2,1)\|FLEXIBLE PIPE(2,1)\|GLOBAL CLIMATE(2,1)\|\|(CN104696005)\|COALBED GAS(100,12)\|OLD GOAF(100,10)\|COAL MINE(100,8)\|COAL MINE OLD GOAF(100,6)\|EXTRACTING RESIDUAL COALBED GAS(100,6)\|RESIDUAL EXTRACTION(100,6)\|SEALING(100,4)\|METHANEDIONE(100,3)\|METHANEDIONE COOPERATIVE SEQUESTRATION(100,1)\|STOPING ROADWAY(84,4)\|METHANEDIONE SEQUESTRATION(73,3)\|RESIDUAL COALBED METHANE(66,4)\|PIPELINE(60,23)\|SEQUESTERING CO OPERATIVE(58,1)\|RESIDUAL COALBED METHANE DEVELOPMENT(57,1)\|GOAF(53,22)\|RESIDUAL COALBED METHANE EXTRACTION(53,2)\|GOAF MIDDLE(52,1)\|METHANEDIONE SEQUESTRATION DOUBLE BENEFIT(51,1)\|EXTRACTION PIPE(46,10)\|ADSORBED CH4AND(46,1)\|WORKING FACE STOPING(43,4)\|WORKING FACE(39,6)\|CH4AND BROKEN COAL(38,1)\|METHANE EXTRACTION(37,1)\|SLIT GROOVE(35,2)\|BAFFLE(33,3)\|SEALING METHANEDIONE(33,2)\|CUTTING HOLE(31,3)\|RESIDUAL COALBED GAS(29,3)\|STOPING(26,4)\|BROKEN COAL ROCK(25,3)\|WORKING FACE STOPING(25,2)\|RESIDUAL COALBED GAS UTILIZATION(25,1)\|PIPE WALL(24,3)\|CLOSURE WALL(22,2)\|PIPELINE2DUE(22,1)\|DUAL BENEFIT(19,1)\|EXTRACTING(18,2)\|CO2THE GAS STORAGE TANK(17,4)\|STOPING LINE(17,4)\|CO2THE AIR STORAGE TANK(16,2)\|NONPRODUCTIVE COAL SEAMS2OUTSTANDING(13,1)\|COMPRESSIVE STRENGTH(12,3)\|WATER INJECTION(10,5)\|PUMP STATION(10,4)\|METHANEDIONE SEQUESTRATION BENEFIT(10,1)\|SEALING WALL(9,6)\|WELL DRILLING(9,6)\|AIR STORAGE TANK(9,3)\|RESIDUAL COALBED METHANE RESOURCE(9,1)\|GAS STORAGE TANK(8,6)\|AIR OUTLET(8,2)\|CO2HAS STRONG ADSORBABILITY(8,1)\|COAL PILLAR CRACK(8,1)\|ADSORBED CH4IS(7,1)\|CH4THE PROMINENCE(7,1)\|CO2FOR DISASTER(6,1)\|COAL SEAM STORE CO2CO(6,1)\|GEOLOGICAL DISPOSAL(6,1)\|MINE ROADWAY(6,1)\|VENTILATION BURDEN(6,1)\|IGNITION PHENOMENON NATURE(5,1)\|INTRODUCING CO2SEALING(5,1)\|RELEVANT SCIENTIST(5,1)\|ABANDONED RESIDUAL(4,1)\|COAL MINING RAPID DEVELOPMENT(4,1)\|COAL RESIDUE(4,1)\|DISPLACING RESIDUAL COALBED GAS(4,1)\|GLOBAL CONCERN(4,1)\|RESIDUAL DISPLACEMENT(4,1)\|STORE CO2IT(4,1)\|ADSORPTIVITY(3,1)\|ATMOSPHERE2THE(3,1)\|DUCT SLOT(3,1)\|GOAF4THE GAS EXTRACTION(3,1)\|LIVING ENVIRONMENT(3,1)\|PIPE PROTECTION(3,1)\|PRIMARY GREENHOUSE(3,1)\|SIGNIFICANCE(3,1)\|UNSAFE FACTOR(3,1)\|ADDITIVE(2,1)\|CH4AND(2,1)\|COAL ROCK MASS PAIR(2,1)\|COALBED GAS INDUSTRY(2,1)\|FACE EXTRACTION(2,1)\|FLEXIBLE PIPE(2,1)\|GLOBAL CLIMATE(2,1)\|	(CN104696005)\|1. The method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in the old goaf of the coal mine is characterized by comprising the following steps:\|a. in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) from a position 5-10 m away from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5);\|b. tightly winding a high-pressure hose (7) with the diameter of 5-15 cm and the compressive strength of 5-10 MPa on the slot (5), injecting 2-5 MPa high-pressure water into the high-pressure hose (7) when all pipelines (4) wound with the high-pressure hose (7) enter a goaf (8), and bundling a water injection port of the high-pressure hose (7) after water injection is finished;\|c. after the stoping of the working face (1) is finished, a closed wall (10) with the thickness of 2-5 m is arranged at the stoping line (9), and the pipeline (4) penetrates through the closed wall (10) and is connected to the ground (11) and the CO2A gas storage tank (12) is communicated with CO2A first valve (13) is arranged at an air outlet of the air storage tank (12);\|d. constructing a well (14) downwards from the ground (11) every 200-300 m along the middle of the goaf (8) until the bottom of the well (14) is 20-40 m away from the upper part of the goaf (8), inserting an extraction pipe (16) into the well (14) from the ground (11), and arranging a second valve (17) at the upper end of the extraction pipe (16);\|after the well mouth of the drilling well (14) is sealed, an extraction pipe (16) is connected with a pump station (15);\|e. opening a first valve (13) by CO2The gas storage tank (12) injects CO into the goaf (8) along the pipeline (4)2Simultaneously opening a second valve (17) to begin extracting CO in the goaf (8)2Displacing residual coal bed gas;\|f. when extracting CO in the pipe (16)2When the concentration is higher than 10%, the first valve (13) and the second valve (17) are closed, and the CO injection is stopped2And extracting residual coal bed gas.	(CN104696005)\|TECHNICAL FIELD\|[0002] The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction, which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf.\|BACKGROUND ART\|[0004] As global climate warms up, asCO, the main greenhouse gas2Disposal issues have become a focus of global concern to relevant scientists. To solve CO2For disasters brought to the living environment of human beings, geological disposal is well known as one of effective ways for solving the problem of influence of greenhouse gas on the environment. Wherein the deep non-recoverable coal seam stores CO2CO considered most economical2Disposal by injecting CO into the non-productive coal seam2Not only can geologically store CO2It can also be used for clean energy source-coal bed gas (CH)4) And (4) recovering.\|[0005] However, with the rapid development of coal mining technology, these non-productive coal seams will become productive in the future, and the CO brought by the non-productive coal seams2Outstanding problem will be better than CH4The prominence is more serious.\|[0006] The large-area old dead zone brought by coal mining is a natural excellent gas storage tank and is also a great risk source threatening safety production, and a large amount of high-concentration gas stored in the large-area old dead zone possibly enters a mining area or a mine roadway through a sealing wall or a coal pillar crack under the action of ventilation negative pressure and the change of atmospheric pressure, so that the ventilation burden and unsafe factors are increased. Therefore, the method is very necessary for extracting the gas in the old goaf, and if the gas is reasonably developed and utilized, the abundant high-concentration gas has extremely important significance for the development of the coal bed gas industry. At present, the gas extraction in the old goaf of the coal mine in China is not ideal, so that a method for reasonably sealing and storing CO is urgently needed2And can also improve the gas extraction rate of the goaf.\|DISCLOSURE\|[0007] Disclosure of Invention\|[0008] The invention aims to solve the problems of old goaf sealing of carbon dioxide and low extraction efficiency of residual coalbed methane in the old goaf, and provides a method for cooperatively sealing carbon dioxide in the old goaf of a coal mine to extract residual coalbed methane.\|[0009] The technical scheme of the invention is as follows: the method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in the old goaf of the coal mine comprises the following specific steps:\|[0010] a. in the working face stoping process, pipelines with the diameter of 30-50 cm are laid at the bottom of a stoping roadway from a position 5-10 m away from a cutting hole, 4 slots which are axially parallel to the pipelines and symmetrically distributed are arranged on the pipe wall of each pipeline every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles with the height of 15-25 cm are arranged at two ends of each slot.\|[0011] b. And tightly winding a high-pressure hose with the diameter of 5-15 cm and the compressive strength of 5-10 MPa on the slot. When all the pipelines wound with the high-pressure hoses enter a mining area, 2-5 MPa of high-pressure water is injected into the high-pressure hoses, and a water injection port of the high-pressure hoses is bound after water injection is finished.\|[0012] c. And after the stoping of the working face is finished, a sealing wall with the thickness of 2-5 m is arranged at the stoping line. The pipeline passes through the sealed wall and is connected to the ground and CO2The gas storage tank is communicated, and a gas outlet of the gas storage tank is provided with a first valve.\|[0013] d. And (3) drilling a well downwards from the ground every 200-300 m along the middle part of the goaf until the bottom of the drilling well is 20-40 m away from the upper part of the goaf, inserting an extraction pipe into the drilling well from the ground, and arranging a second valve at the upper end of the extraction pipe. And after the well mouth of the well is sealed, the extraction pipe is connected with a pump station.\|[0014] e. Opening a first valve by CO2The gas storage tank injects CO into the goaf along the pipeline2. Simultaneously opening a second valve to begin extracting CO in the goaf2And (4) displacing residual coal bed gas.\|[0015] f. When extracting CO in the pipe2When the concentration is higher than 10%, the first valve and the second valve are closed, and CO injection is stopped2And extracting residual coal bed gas.\|[0016] The invention has the beneficial effects that:\|[0017] (1) the high-pressure flexible pipe protection technology is adopted, water with certain pressure is injected into the flexible pipe, so that the pipeline is protected in a pressure yielding mode, and the broken coal rocks are prevented from damaging the pipeline and blocking air holes;\|[0018] (2) by using CO2Density ofGreater than CH4And crushing coal rock mass pair CO at the top of the goaf2The characteristic of greater adsorptivity, in injecting CO into the goaf2In the process of (A), CO2Firstly occupying the space at the lower part of the goaf and crushing the original adsorbed CH of the coal rock mass4Is displaced and gradually moves upwards to the top of the goaf for accumulation, and then the drilling well is used for drilling CH in the goaf4The gas extraction efficiency of the goaf is greatly improved by extraction;\|[0019] (3) introducing CO2Sealing and storing the waste gas in the old goaf of the coal mine, thereby not only reducing the emission of CO to the atmosphere2The amount of the additive is reduced, the greenhouse effect is relieved, the natural ignition phenomenon of the residual coal in the old goaf can be effectively inhibited, and the safety of a mine is enhanced;\|[0020] (4) the originally abandoned residual coalbed methane resources in the goaf are developed and utilized, and the method has double benefits of carbon dioxide sequestration and development and utilization of the residual coalbed methane resources.\|DRAWINGS DESCRIPTION\|[0022] FIG. 1 is a schematic view of a pipeline laid during the face extraction process\|[0023] FIG. 2 is a schematic diagram of the principle of the present invention\|[0024] FIG. 3 is a schematic view of a duct slot\|[0025] FIG. 4 is a cross-sectional view taken along line A-A in FIG. 3\|[0026] In the figure: 1-working face, 2-cutting hole, 3-mining roadway, 4-pipeline, 5-slot,\|[0027] 6-baffle, 7-high pressure hose, 8-goaf, 9-stoping line, 10-sealing wall,\|[0028] 11-ground, 12-CO2Gas storage tank, 13-first valve, 14-drilling well, 15-pump station,\|[0029] 16-an extraction pipe, 17-a second valve.\|INVENTION MODE\|[0030] Detailed Description\|[0031] Examples of the invention are further described below with reference to the accompanying drawings:\|[0032] the invention discloses a method for cooperatively sealing carbon dioxide and developing residual coalbed methane in a coal mine goaf, which comprises the following steps: in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) at a distance of 5-10 m from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5). And a high-pressure hose (7) with the diameter of 5-15 cm and the compressive strength of 5-10 MPa is tightly wound on the slot (5). When the pipeline (4) wound with the high-pressure hose (7) completely enters the goaf (8), 2-5 MPa of high-pressure water is injected into the high-pressure hose (7), the pipeline (4) is protected in a yielding manner, the pipeline (4) is prevented from being damaged by broken coal rocks and blocking air holes, and the high-pressure hose (7) is bound after the water injection is finished. After the stoping of the working face (1) is finished, a sealing wall (10) with the thickness of 2-5 m is arranged at the stoping line (9). The pipeline (4) passes through the sealed wall (10) and is connected to the ground (11) and CO2The air storage tank (12) is communicated, and a first valve (13) is arranged at an air outlet of the air storage tank (12). And (3) constructing a well (14) downwards from the ground (11) every 200-300 m along the middle part of the goaf (8) until the bottom of the well (14) is 20-40 m away from the upper part of the goaf (8), inserting an extraction pipe (16) into the well (14) from the ground, and arranging a second valve (17) on the extraction pipe (16). After the well mouth of the drilling well (14) is sealed, the extraction pipe (16) is connected with a pump station (15). Opening the first valve (13) by CO2The gas storage tank (12) injects CO2 into the gob (8) along the pipeline (4). During injection, due to CO2Density greater than CH4,CO2Firstly occupying the space at the lower part of the goaf (8), and crushing coal rocks at the top of the goaf (8) to CO2Has stronger adsorbability, namely the original adsorbed CH4Is displaced and gradually moves upwards to the top of the goaf (8) for accumulation. And opening a second valve (17) to begin extracting residual coal bed gas in the goaf (8). When extracting CO in the pipe (16)2When the concentration is higher than 10%, the first valve (13) and the second valve (17) are closed, and the CO injection is stopped2And extracting residual coal bed gas.	(CN104696005)\|TECHNICAL FIELD\|[0002] The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction, which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf.\|BACKGROUND ART\|[0004] As global climate warms up, asCO, the main greenhouse gas2Disposal issues have become a focus of global concern to relevant scientists. To solve CO2For disasters brought to the living environment of human beings, geological disposal is well known as one of effective ways for solving the problem of influence of greenhouse gas on the environment. Wherein the deep non-recoverable coal seam stores CO2CO considered most economical2Disposal by injecting CO into the non-productive coal seam2Not only can geologically store CO2It can also be used for clean energy source-coal bed gas (CH)4) And (4) recovering.\|[0005] However, with the rapid development of coal mining technology, these non-productive coal seams will become productive in the future, and the CO brought by the non-productive coal seams2Outstanding problem will be better than CH4The prominence is more serious.\|[0006] The large-area old dead zone brought by coal mining is a natural excellent gas storage tank and is also a great risk source threatening safety production, and a large amount of high-concentration gas stored in the large-area old dead zone possibly enters a mining area or a mine roadway through a sealing wall or a coal pillar crack under the action of ventilation negative pressure and the change of atmospheric pressure, so that the ventilation burden and unsafe factors are increased. Therefore, the method is very necessary for extracting the gas in the old goaf, and if the gas is reasonably developed and utilized, the abundant high-concentration gas has extremely important significance for the development of the coal bed gas industry. At present, the gas extraction in the old goaf of the coal mine in China is not ideal, so that a method for reasonably sealing and storing CO is urgently needed2And can also improve the gas extraction rate of the goaf.\|DISCLOSURE\|[0007] Disclosure of Invention\|[0008] The invention aims to solve the problems of old goaf sealing of carbon dioxide and low extraction efficiency of residual coalbed methane in the old goaf, and provides a method for cooperatively sealing carbon dioxide in the old goaf of a coal mine to extract residual coalbed methane.\|[0009] The technical scheme of the invention is as follows: the method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in the old goaf of the coal mine comprises the following specific steps:\|[0010] a. in the working face stoping process, pipelines with the diameter of 30-50 cm are laid at the bottom of a stoping roadway from a position 5-10 m away from a cutting hole, 4 slots which are axially parallel to the pipelines and symmetrically distributed are arranged on the pipe wall of each pipeline every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles with the height of 15-25 cm are arranged at two ends of each slot.\|[0011] b. And tightly winding a high-pressure hose with the diameter of 5-15 cm and the compressive strength of 5-10 MPa on the slot. When all the pipelines wound with the high-pressure hoses enter a mining area, 2-5 MPa of high-pressure water is injected into the high-pressure hoses, and a water injection port of the high-pressure hoses is bound after water injection is finished.\|[0012] c. And after the stoping of the working face is finished, a sealing wall with the thickness of 2-5 m is arranged at the stoping line. The pipeline passes through the sealed wall and is connected to the ground and CO2The gas storage tank is communicated, and a gas outlet of the gas storage tank is provided with a first valve.\|[0013] d. And (3) drilling a well downwards from the ground every 200-300 m along the middle part of the goaf until the bottom of the drilling well is 20-40 m away from the upper part of the goaf, inserting an extraction pipe into the drilling well from the ground, and arranging a second valve at the upper end of the extraction pipe. And after the well mouth of the well is sealed, the extraction pipe is connected with a pump station.\|[0014] e. Opening a first valve by CO2The gas storage tank injects CO into the goaf along the pipeline2. Simultaneously opening a second valve to begin extracting CO in the goaf2And (4) displacing residual coal bed gas.\|[0015] f. When extracting CO in the pipe2When the concentration is higher than 10%, the first valve and the second valve are closed, and CO injection is stopped2And extracting residual coal bed gas.\|[0016] The invention has the beneficial effects that:\|[0017] (1) the high-pressure flexible pipe protection technology is adopted, water with certain pressure is injected into the flexible pipe, so that the pipeline is protected in a pressure yielding mode, and the broken coal rocks are prevented from damaging the pipeline and blocking air holes;\|[0018] (2) by using CO2Density ofGreater than CH4And crushing coal rock mass pair CO at the top of the goaf2The characteristic of greater adsorptivity, in injecting CO into the goaf2In the process of (A), CO2Firstly occupying the space at the lower part of the goaf and crushing the original adsorbed CH of the coal rock mass4Is displaced and gradually moves upwards to the top of the goaf for accumulation, and then the drilling well is used for drilling CH in the goaf4The gas extraction efficiency of the goaf is greatly improved by extraction;\|[0019] (3) introducing CO2Sealing and storing the waste gas in the old goaf of the coal mine, thereby not only reducing the emission of CO to the atmosphere2The amount of the additive is reduced, the greenhouse effect is relieved, the natural ignition phenomenon of the residual coal in the old goaf can be effectively inhibited, and the safety of a mine is enhanced;\|[0020] (4) the originally abandoned residual coalbed methane resources in the goaf are developed and utilized, and the method has double benefits of carbon dioxide sequestration and development and utilization of the residual coalbed methane resources.\|DRAWINGS DESCRIPTION\|[0022] FIG. 1 is a schematic view of a pipeline laid during the face extraction process\|[0023] FIG. 2 is a schematic diagram of the principle of the present invention\|[0024] FIG. 3 is a schematic view of a duct slot\|[0025] FIG. 4 is a cross-sectional view taken along line A-A in FIG. 3\|[0026] In the figure: 1-working face, 2-cutting hole, 3-mining roadway, 4-pipeline, 5-slot,\|[0027] 6-baffle, 7-high pressure hose, 8-goaf, 9-stoping line, 10-sealing wall,\|[0028] 11-ground, 12-CO2Gas storage tank, 13-first valve, 14-drilling well, 15-pump station,\|[0029] 16-an extraction pipe, 17-a second valve.\|INVENTION MODE\|[0030] Detailed Description\|[0031] Examples of the invention are further described below with reference to the accompanying drawings:\|[0032] the invention discloses a method for cooperatively sealing carbon dioxide and developing residual coalbed methane in a coal mine goaf, which comprises the following steps: in the stoping process of the working face (1), pipelines (4) with the diameter of 30-50 cm are laid at the bottom of a stoping roadway (3) at a distance of 5-10 m from a cutting hole (2), 4 slots (5) which are axially parallel to the pipelines (4) and symmetrically distributed are arranged on the pipe wall of the pipelines (4) every 10-20 m, the length of each slot is 1-3 m, the width of each slot is 0.5-3 cm, and baffles (6) with the height of 15-25 cm are arranged at two ends of each slot (5). And a high-pressure hose (7) with the diameter of 5-15 cm and the compressive strength of 5-10 MPa is tightly wound on the slot (5). When the pipeline (4) wound with the high-pressure hose (7) completely enters the goaf (8), 2-5 MPa of high-pressure water is injected into the high-pressure hose (7), the pipeline (4) is protected in a yielding manner, the pipeline (4) is prevented from being damaged by broken coal rocks and blocking air holes, and the high-pressure hose (7) is bound after the water injection is finished. After the stoping of the working face (1) is finished, a sealing wall (10) with the thickness of 2-5 m is arranged at the stoping line (9). The pipeline (4) passes through the sealed wall (10) and is connected to the ground (11) and CO2The air storage tank (12) is communicated, and a first valve (13) is arranged at an air outlet of the air storage tank (12). And (3) constructing a well (14) downwards from the ground (11) every 200-300 m along the middle part of the goaf (8) until the bottom of the well (14) is 20-40 m away from the upper part of the goaf (8), inserting an extraction pipe (16) into the well (14) from the ground, and arranging a second valve (17) on the extraction pipe (16). After the well mouth of the drilling well (14) is sealed, the extraction pipe (16) is connected with a pump station (15). Opening the first valve (13) by CO2The gas storage tank (12) injects CO2 into the gob (8) along the pipeline (4). During injection, due to CO2Density greater than CH4,CO2Firstly occupying the space at the lower part of the goaf (8), and crushing coal rocks at the top of the goaf (8) to CO2Has stronger adsorbability, namely the original adsorbed CH4Is displaced and gradually moves upwards to the top of the goaf (8) for accumulation. And opening a second valve (17) to begin extracting residual coal bed gas in the goaf (8). When extracting CO in the pipe (16)2When the concentration is higher than 10%, the first valve (13) and the second valve (17) are closed, and the CO injection is stopped2And extracting residual coal bed gas.	Family Number\|(69557757)\|69557757\|Object of Invention\|(CN104696005B B)\|The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction , which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf . \|(CN104696005 A)\|The invention relates to a method for carbon dioxide sequestration and residual coalbed methane extraction , which is particularly suitable for the cooperative sequestration of carbon dioxide and the development of residual coalbed methane in a coal mine goaf . \|Abstract\|(CN104696005B B)\|The invention discloses a method for synchronously extracting residual coalbed methane and sealing and preserving carbon dioxide in an old coal mined - out area of coal mine . The method comprises the following steps : during working face mining , a pipeline is paved at the bottom of a mining roadway , seam grooves are axially formed in the pipeline at intervals , baffles are arranged on both ends of each seam groove , high - pressure hoses are respectively wound on the seam grooves , water under a certain pressure is injected in the high - pressure hoses to perform & apos ; yielding&apos ; protection on the pipeline , so that crushed coal and rock in the mined - out area can be prevented from destroying the pipeline and blocking air holes ; after working face mining is finished , a fire dam is arranged at a mining stop line , the pipeline is communicated to the ground , and well drilling is constructed from the ground to the upper part of the mined - out area ; CO2 is injected from the ground to the mined out area along the pipeline , because the density of the CO2 is larger than CH4 , and the crushed coal and rock remained at the bottom of the mined - out area has higher adsorptivity to CO2 , the absorbed CH4 is replaced out and is accumulated at the top of the mined - out area , and the accumulated CH4 is extracted by well drilling . The method has dual benefits of sealing and preserving the carbon dioxide , and developing and utilizing the residual coalbed methane . \|	Civil engineering	E21B-041/00/64\|E21B-043/00/6\|E21B-043/16/4\|E21F-007/00\|Y02P-090/70		E21B-041/00/64\|E21B-043/00/6\|E21B-043/16/4\|E21F-007/00\|Y02P-090/70	E21B-043/16\|E21F-007/00	E21B-043/16\|E21F-007/00			CN112943347\|CN110608022\|CN109488269B\|CN119145824B\|CN116575900B\|CN115492557B\|CN113027511B\|CN105797570B	CN112943347 94683113 WHO=Examiner SELF=Y CAT=A\|CN110608022 87065712 WHO=Examiner SELF=N CAT=A\|CN109488269B 83753115 WHO=Examiner SELF=N CAT=A\|CN119145824B 112657834 WHO=Examiner SELF=N\|CN116575900B 106093745 WHO=Examiner SELF=Y\|CN115492557B 103072638 WHO=Examiner SELF=N\|CN113027511B 101827199 WHO=Examiner SELF=N\|CN105797570B 73701055 WHO=Examiner SELF=N	CN102877819\|CN103670338\|CN102587958\|CN102226412\|RU2445462\|CN101418679	CN102877819 8051501 WHO=Examiner SELF=N CAT=A\|CN103670338 64988101 WHO=Examiner SELF=N CAT=A\|CN102587958 7811393 WHO=Examiner SELF=N CAT=A\|CN102226412 7462754 WHO=Examiner SELF=N CAT=A\|RU2445462 36341417 WHO=Examiner SELF=N CAT=A\|CN101418679 6743135 WHO=Examiner SELF=Y CAT=A		CN101418679; CN102226412; RU2445462; CN102587958; CN102877819; CN103670338		GRANTED	(CN104696005)\|GRANTED	ALIVE	(CN104696005)\|ALIVE	(CN104696005)\|LEGAL DETAILS FOR CN104696005\|Actual or expected expiration date=2035-02-03\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2015-02-03\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201510055353\|Application date=2015-02-03\|Standardized application number=2015CN-0055353\|Event publication date=2015-06-10\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN104696005\|Publication stage code=A\|Publication date=2015-06-10\|Standardized publication number=CN104696005\|Event publication date=2015-06-10\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2015-07-08\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2016-08-31\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN104696005\|Publication stage code=B\|Publication date=2016-08-31\|Standardized publication number=CN104696005B\|Event publication date=2016-08-31\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right		(CN104696005)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=tO7C931onjmjLykQKxGtiRj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000013731776&ekey=2330&xpn=CN104696005B&kind=B	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=eoY4Iua8XF2Kfx%252FE0Z3k1rmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN104696005)\|CN	(CN104696005)\|NAME=TAIYUAN UNIVERSITY OF TECHNOLOGY , COUNTRY=CN		(CN104696005)\|NAME=LU MAOCHUN;KERUIDA PATENT AGENCY CO., LTD. TAIYUAN CITY , REG=14101\|(CN104696005)\|NAME=LU MAOCHUN;KERUIDA PATENT AGENCY CO., LTD. TAIYUAN CITY		(CN104696005)\|NAME=HU SHENGYONG\|NAME=GAO QIANG\|NAME=CHEN CHUNJIAN\|NAME=ZHANG XIANG\|(CN104696005)\|NAME=HU SHENGYONG\|NAME=GAO QIANG\|NAME=CHEN CHUNJIAN\|NAME=ZHANG XIANG	(CN104696005)\|4	1	1					(CN104696005)\|Number of Claims: NCL=1\|Gazette date: GAZDATE=2016-08-31\|Gazette number: GAZNUM=32-35\|Number of Pages: NPAGES=7\|Primary examiner: 隗敏\|Primary examiner: Kui Min\|\|(CN104696005)\|Number of Claims: NCL=1\|Gazette date: GAZDATE=2015-06-10\|Gazette number: GAZNUM=31-24\|Number of Pages: NPAGES=7\|Primary examiner: 隗敏\|Primary examiner: Kui Min\|		(CN104696005)\|CHINESE (CHI)	(CN104696005B)\|Patent\|(CN104696005)\|Patent	Titre: (CN104696005)\|Method for extracting residual coal bed gas by cooperatively sealing and storing carbon dioxide in old goaf of coal mine Résumé: (CN104696005)\|The invention discloses a method for synchronously extracting residual coalbed methane and sealing and preserving carbon dioxide in an old coal mined-out area of coal mine. The method comprises the following steps: during working face mining, a pipeline is paved at the bottom of a mining roadway, seam grooves are axially formed in the pipeline at intervals, baffles are arranged on both ends of each seam groove, high-pressure hoses are respectively wound on the seam grooves, water under a certain pressure is injected in the high-pressure hoses to perform 'yielding' protection on the pipeline, so that crushed coal and rock in the mined-out area can be prevented from destroying the pipeline and blocking air holes; after working face mining is finished, a fire dam is arranged at a mining stop line, the pipeline is communicated to the ground, and well drilling is constructed from the ground to the upper part of the mined-out area; CO2 is injected from the ground to the mined out area along the pipeline, because the density of the CO2 is larger than CH4, and the crushed coal and rock remained at the bottom of the mined-out area has higher adsorptivity to CO2, the absorbed CH4 is replaced out and is accumulated at the top of the mined-out area, and the accumulated CH4 is extracted by well drilling. The method has dual benefits of sealing and preserving the carbon dioxide, and developing and utilizing the residual coalbed methane.	33	Abstract	gpt-4o-mini	no	The article focuses on extracting methane and sealing carbon dioxide in a mined area, without addressing the accelerated weathering of minerals or carbon sequestration through mineral alteration.
36	CN202110837467	CN202110837467	CN113494265\|CN113494265	96423759	CN113494265 B 2023-05-02 [CN113494265B]\|CN113494265 A 2021-10-12 [CN113494265]	2021-07-23	2021-07-23	2023-05-02\|2021-10-12	(CN113494265B)\|2023-05-02	(CN113494265)\|2025-07-18	(CN113494265)\|Plugging method for leakage along abandoned well in carbon dioxide geological storage process	(CN113494265)\|The invention provides a method for blocking leakage along an abandoned well in the geological storage process of carbon dioxide. The method comprises the following steps that perforating is carried out by adopting a stable cover layer above a geological storage layer of carbon dioxide; a shaft with leakage risk, drilling annular cement and a surrounding rock fracture zone communicate with one another; and lime milk turbid liquid is injected into a perforation interval, so that lime milk in a gap reacts with leaked carbon dioxide to form hardened and compact calcium carbonate, and a carbon dioxide leakage channel is blocked. According to the method for blocking leakage along the abandoned well in the geological storage process of carbon dioxide, the crack channel leaking along the abandoned well in the geological storage process of carbon dioxide can be effectively blocked, meanwhile, a surrounding rock broken zone and crack-containing drilling well annulus cement can be cemented into a compact whole, and the risk of leaking along the abandoned well in the geological storage process of carbon dioxide is greatly reduced. The injected lime milk turbid liquid reacts with carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, the geological environment pollution risk is extremely low, and the plugging process is safe and environmentally friendly.	CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS	(CN113494265)\|CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS ([CN])\|(CN113494265)\|CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS ([CN])	FU LEI\|MA XIN\|DIAO YUJIE\|ZHANG CHENGLONG\|LIU TING\|Fu Jie\|SHAO WEI	(CN113494265)\|FU LEI\|MA XIN\|DIAO YUJIE\|ZHANG CHENGLONG\|LIU TING\|Fu Jie\|SHAO WEI\|(CN113494265)\|FU LEI\|MA XIN\|DIAO YUJIE\|ZHANG CHENGLONG\|LIU TING\|Fu Jie\|SHAO WEI	(CN113494265)\|CHEN YING;BEIJING BEIXIN-ZHICHENG INTELLECTUAL PROPERTY AGENT CO., LTD.\|Reg. Nb: 11100	(CN113494265)\|At present, great project demonstration of carbon capture utilization and sealing is developed in each industry of China, and a foundation is laid for subsequent large-scale carbon dioxide injection.\|It is also a good measure that the perforation segments are evenly distributed over the entire circumference of the inner wall of the well.\|According to the invention, lime milk is injected into the perforation of the cover layer, and on annular cement and surrounding rock fracture zones where cracks appear due to the damage of drilling on the cover layer, the lime milk and carbon dioxide meet and react in the cracks to generate calcium carbonate to fill and seal the cracks, so that the cover layer is repaired.\|However, if the initial set concentration is too high, the lime milk is too thick, and besides the problems of the above and the increase of the concentration reduction times, ports of some cracks are sealed by the thick lime milk, so that the whole annular cement and the size cracks in the surrounding rock breaking zone are not filled, and the sealing effect is also affected.\|The injection rate described above also affects the occlusion effect.\|	(CN113494265)\|1. A plugging method for leakage along an abandoned well in a carbon dioxide geological storage process is characterized by comprising the following steps of: the method comprises the following steps:step 1: perforating, namely perforating a perforating section formed on the inner wall of the shaft corresponding to the thickness of the stable covering layer, and communicating the annular cement of the drilling well with cracks of the surrounding rock breaking zone;step 2: injecting lime milk suspension, namely injecting the lime milk suspension into the perforation, so that the lime milk suspension enters the crack and reacts with leaked carbon dioxide to form calcium carbonate, and further plugging a leakage channel of the carbon dioxide;the plugging method further comprises at least one of the following steps:prior to step 1, comprising:a leakage identification step of identifying whether or not the abandoned well has carbon dioxide leaked along the well; and/or the number of the groups of groups,cleaning the inside of the well, namely cleaning a sealing bridge plug in the well before sealing the leaked abandoned well, and ensuring the smoothness and smoothness of the inner wall of the well shaft above the carbon dioxide geological sealing storage layer;and/or the number of the groups of groups,after step 2, it includes:a plugging effect monitoring step, namely monitoring the plugging effect of the well drilling after plugging; and/or, well sealing, namely, sealing the well by an in-well bridge plug for the well drilling after the well is plugged;in the step (1) of the process,before perforation, a relatively closed space is arranged in the well corresponding to the cover layer part, and the perforation section is arranged in the space; and/or the number of the groups of groups,in the step 2 of the process, the process is carried out,injecting lime milk suspension through a fracturing truck; and/or when injection begins, the injection pressure P is less than the reservoir pressure P 0 When the concentration of the lime milk suspension is an initial set concentration, and when P is larger than P 0 When the concentration of the lime milk suspension is reduced at a threshold value, the lime milk suspension is continuously injected, and when P is larger than P again 0 And when the threshold value is reached, the concentration of the lime milk suspension is reduced again, then the injection is continued until the concentration of the lime milk suspension is equal to a final set concentration, namely, the injection is continued at the final set concentration until the injection pressure P reaches an injection termination set pressure, and the injection is ended.\|	(CN113494265)\|The invention provides a maximum rate limit of 0.5 liter/second at which lime milk entering the crack can react with leaked carbon dioxide in good time to form calcium carbonate to seal the crack.\|The invention provides a plugging method for leakage along an abandoned well in a carbon dioxide geological storage process, which comprises the steps of perforating a stable cover layer on a carbon dioxide geological storage layer, communicating a shaft with leakage risk, drilling annular cement and a surrounding rock breaking belt, injecting lime milk suspension into a perforation section, enabling lime milk in a gap to react with leaked carbon dioxide to form hardened and compact calcium carbonate, and plugging a carbon dioxide leakage channel.\|	(CN113494265)\|CARBON DIOXIDE(100,110)\|LIME MILK SUSPENSION(100,57)\|PLUGGING(100,38)\|WELL ABANDONMENT(100,30)\|LEAKAGE(100,12)\|GEOLOGICAL STORAGE(100,3)\|CARBON DIOXIDE GEOLOGICAL STORAGE(100,1)\|GEOLOGICAL STORAGE(100,1)\|ANNULAR CEMENT(48,12)\|ROCK BREAKING ZONE(47,8)\|ANTILEAKAGE BRIDGE PLUGIN(44,1)\|DRILLING ANNULUS PERMEABILITY(40,1)\|SEALING BRIDGE PLUGIN(39,2)\|PLUGGING BRIDGE PLUGIN(37,1)\|PERFORATION SEGMENT(33,1)\|PERFORATING SECTION(32,27)\|LEAKAGE IDENTIFICATION(32,4)\|FRACTURING TRUCK(30,4)\|CARBON CAPTURE UTILIZATION DEMONSTRATION(30,1)\|CRACK(29,21)\|CORROSION RESISTANT CEMENT(29,6)\|INJECTED LIME MILK SUSPENSION(29,5)\|CRACK PORT(29,1)\|PERFORATION(27,20)\|ABANDONED BOREHOLE SONIC LOGGING(27,2)\|DRILLING DAMAGE(27,1)\|GEOLOGICAL ENVIRONMENT POLLUTION(26,3)\|THICK LIME MILK(26,1)\|LIME MILK(25,26)\|COVER LAYER(24,34)\|GEOLOGICAL SEALING(24,5)\|SMOOTHNESS(24,4)\|DRILLING ANNULAR CEMENT(24,2)\|POZZOLAN CEMENT(23,2)\|ROCK FRACTURE ZONE(22,8)\|BRIDGE PLUG(22,2)\|OVERLYING STRATUM(22,2)\|CALCIUM CARBONATE(21,15)\|PACKER INSTALLATION(21,2)\|CARBON DIOXIDE GEOLOGICAL SEALING(20,3)\|ANALYZING LOGGING(20,2)\|BRIDGE PLUG IN(20,2)\|RESERVOIR(19,16)\|GEOLOGICAL STORAGE LAYER(19,2)\|LIME MILK SUSPENSION INJECTION(18,3)\|FOUNDATION(18,1)\|PIPE ORIFICE(18,1)\|UTILIZING CARBON CAPTURE(18,1)\|FULL CIRCUMFERENCE(17,1)\|INJECTION PRESSURE(16,16)\|UPPER PACKER(16,8)\|CEMENT COMPOSITE(16,3)\|FLY ASH CEMENT(16,3)\|WELLHEAD PERIMETER CARBON DIOXIDE(16,3)\|CAP LAYER(15,15)\|CRACK CHANNEL(15,3)\|CARBON DIOXIDE INJECTION(15,1)\|CARBON DIOXIDE MEET(15,1)\|CALCIUM HYDROXIDE SOLUBILITY(14,2)\|SIZE CRACK(14,1)\|LEAKAGE RISK(13,8)\|PACKER DISTANCE(13,7)\|DRILLING ANNULUS CEMENT(12,3)\|DRILLING WELL ANNULAR CEMENT(12,2)\|INJECTION PIPE(11,7)\|LEAKAGE CHANNEL(11,6)\|COMPACT WHOLE(11,5)\|LIME MILK SUSPENSION SET(11,4)\|STABLE COVERING LAYER(11,4)\|INJECTION RATE(11,2)\|INJECTION SPEED(11,1)\|LIME MILK SATURATED SOLUTION(11,1)\|THRESHOLD VALUE(10,17)\|ROCK(10,4)\|CORRELATION(10,2)\|LEAKED ABANDONED WELL(10,2)\|LOGGING DATA(10,2)\|MONITORING PERIOD(10,2)\|RESERVOIR LAYER(10,2)\|CARBON DIOXIDE LEAKAGE PATH(10,1)\|FINAL SET(9,11)\|STABLE COVER LAYER(9,5)\|PERFORATED SECTION(9,4)\|STABLE COVERING LAYER THICKNESS(9,4)\|STORAGE LAYER(9,4)\|MONITORING FREQUENCY(9,3)\|SLAG CEMENT(9,3)\|CARBON DIOXIDE(9,1)\|WELL DRILLING(8,11)\|INJECTION TERMINATION SETTING PRESSURE(8,2)\|PH VALUE PROBE(8,2)\|RESERVOIR PRESSURE(8,2)\|EVENLY DISTRIBUTED OVER(8,1)\|UPPER EDGE(7,9)\|PRESSURE DIFFERENCE(7,5)\|CARBON DIOXIDE LEAKAGE CHANNEL(7,4)\|CONSTANT VALUE(7,4)\|LEAK IDENTIFICATION(7,4)\|BLOWOUT PREVENTION PROTECTION DEVICE(7,3)\|CARBON DIOXIDE RESERVOIR TEMPERATURE(7,2)\|DRILLING MACHINE(7,2)\|BOREHOLE ANNULUS CEMENT(7,1)\|CEMENT BRIDGE PLUGIN(7,1)\|OCCLUSION EFFECT(7,1)\|INNER WALL(6,9)\|PERFORATING SECTION HEIGHT(6,7)\|FORMATION TEMPERATURE(6,5)\|CARBON DIOXIDE SEALING(6,4)\|EXHAUST VALVE(6,4)\|SAFE(6,3)\|CARBON DIOXIDE GEOLOGICAL SEQUESTRATION(6,2)\|CEMENT SHEATH(6,2)\|OVERBURDEN STRATUM(6,1)\|OVERBURDEN WEAKNESS(6,1)\|WELL SHAFT(5,7)\|INJECTION TERMINATION SET PRESSURE(5,4)\|FINE CRACK(5,3)\|ABANDONED DRILLING WELL(5,2)\|CIRCUMFERENTIAL SURFACE(5,2)\|PLUGGING LEAKAGE(5,2)\|ANNULUS PERMEABILITY(5,1)\|CALCULATED STRATUM PERMEABILITY(5,1)\|LEAKAGE PROOF BRIDGE PLUGIN(5,1)\|MAXIMUM RATE LIMIT(5,1)\|WELLBORE BRIDGE PLUG(5,1)\|WELLHEAD GAS FLOWMETER(5,1)\|WELLHEAD VENT VALVE(5,1)\|WELL SEALING(4,4)\|CARBON NEUTRALIZATION(4,2)\|STIRRING BOX(4,2)\|MONITORING PLUGGING(4,1)\|REPAIRING DIFFICULTY(4,1)\|VOLCANIC ASH CEMENT(4,1)\|CONCENTRATION REDUCTION TIME(3,2)\|CONTINUITY(3,2)\|FORMATION WATER(3,2)\|LAYER PROTECTION(3,2)\|ABANDONED HYDROCARBON RESERVOIR(3,1)\|ABANDONED WELLBORE(3,1)\|BLOWOUT PREVENTER COMPONENT(3,1)\|CLAY CONTENT(3,1)\|FOSSIL ENERGY(3,1)\|GEOLOGICAL SEAL STORAGE(3,1)\|GREENHOUSE GAS GEOLOGICAL SEALING(3,1)\|HARDENED COMPACT CALCIUM CARBONATE(3,1)\|IDENTIFYING LEAKAGE(3,1)\|INJECTING LIME MILK(3,1)\|LEAKAGE REASON(3,1)\|LEAKAGE SEALING(3,1)\|LIME MILK REACTION(3,1)\|LIME MILK SUSPENSION REACTION(3,1)\|LIME SUSPENSION(3,1)\|OVERLYING STRATUM WATER(3,1)\|PERFORATION INTERVAL(3,1)\|SUDDEN LEAKAGE(3,1)\|\|(CN113494265)\|CARBON DIOXIDE(100,110)\|LIME MILK SUSPENSION(100,55)\|WELL ABANDONMENT(100,24)\|BLOCKING LEAKAGE(100,4)\|CARBON DIOXIDE SEQUESTRATION(100,4)\|CARBON DIOXIDE SEQUESTRATION(100,3)\|SEQUESTRATION(100,3)\|PLUGGING LEAKAGE(100,1)\|ROCK CRUSHING ZONE(59,1)\|DRILLING ANNULAR CEMENT(43,2)\|INJECTING LIME MILK(38,8)\|DRILLING ANNULUS PERMEABILITY(38,2)\|PLUGGING(37,34)\|ANNULAR CEMENT(36,12)\|BLOCKING BRIDGE PLUGIN(36,1)\|PLUGGING BRIDGE PLUGIN(34,3)\|LEAK PROOF BRIDGE PLUGIN(34,1)\|PERFORATION(33,22)\|ROCK FRACTURE ZONE(33,15)\|CORROSION RESISTANT CEMENT(33,6)\|BRIDGE PLUG IN(33,4)\|OVERBURDEN STRATUM(32,2)\|SUDDEN LEAKAGE(32,1)\|ABANDONED BOREHOLE SONIC LOGGING(31,2)\|PERFORATION SEGMENT(31,2)\|GEOLOGICAL ENVIRONMENT POLLUTION(29,3)\|PERFORATING SECTION(28,26)\|LEAKAGE IDENTIFICATION(28,4)\|HARDENED COMPACT CALCIUM CARBONATE(28,3)\|GEOLOGICAL STORAGE LAYER(28,1)\|GEOLOGICAL SEALING(27,6)\|HARDENED COMPACT(26,3)\|POZZOLAN CEMENT(26,2)\|LIME MILK SUSPENSION SETTING(26,1)\|CEMENT INJECTION(25,1)\|LIME MILK(24,28)\|CALCIUM CARBONATE(24,15)\|FRACTURING TRUCK(24,6)\|UNSATURATED LIME WATER INJECTION(24,1)\|CRACK(23,15)\|ANALYZING LOGGING(23,2)\|WELLHEAD PERIPHERY(22,3)\|LIME MILK SUSPENSION INJECTION(22,2)\|UPPER PACKER(19,8)\|FLY ASH CEMENT(19,3)\|FULL CIRCUMFERENCE(19,1)\|INJECTION PRESSURE(18,17)\|CEMENT COMPOSITE(18,3)\|ROCK BREAKING ZONE(18,3)\|PERFORATED SECTION(18,2)\|UNSATURATED LIME WATER(18,1)\|STABLE COVER LAYER(17,10)\|CARBON DIOXIDE LEAKAGE(17,8)\|CRACK CHANNEL(17,3)\|GEOLOGICAL STORAGE(17,1)\|CAP LAYER(16,7)\|LEAKAGE RISK(16,5)\|CALCIUM HYDROXIDE SOLUBILITY(16,2)\|INJECTION RATE(16,1)\|P0AND P0THE PRESSURE DIFFERENCE(15,2)\|ENVIRONMENTAL PROTECTION(15,1)\|LEAKAGE CHANNEL(14,5)\|FRACTURE(13,7)\|CIRCULATING MODE(13,2)\|LIME MILK SATURATED SOLUTION(13,1)\|INJECTION PIPE(12,7)\|WHOLE SEAL(12,3)\|THRESHOLD VALUE(11,17)\|DRILLING ANNULUS CEMENT(11,2)\|MONITORING PERIOD(11,2)\|P0WHEN(11,2)\|FINAL SET(10,11)\|STABLE COVER LAYER THICKNESS(10,5)\|MONITORING FREQUENCY(10,3)\|SLAG CEMENT(10,3)\|INJECTION SPEED(10,2)\|RESERVOIR PRESSURE(10,2)\|SOLUTION LEVEL(10,1)\|CARBON DIOXIDE LEAKAGE CHANNEL(9,3)\|PH VALUE PROBE(9,3)\|ANTILEAKAGE BRIDGE PLUGIN(9,1)\|EVENLY DISTRIBUTED OVER(9,1)\|UPPER EDGE(8,9)\|CONSTANT VALUE(8,4)\|LEAK IDENTIFICATION(8,4)\|PLUGGED WELL(8,4)\|PLUGGING(8,4)\|BLOWOUT PREVENTION PROTECTION DEVICE(8,2)\|CARBON DIOXIDE RESERVOIR TEMPERATURE(8,2)\|DRILLING MACHINE(8,2)\|CEMENT BRIDGE PLUGIN(8,1)\|LIME MILKTHE SUSPENSION(8,1)\|WELL ROCK FRACTURE ZONE(8,1)\|EXHAUST VALVE(7,4)\|SAFE(7,3)\|CEMENT SHEATH(7,2)\|RESERVOIR STRATUM(7,2)\|GREENHOUSE GAS GEOLOGICAL SEQUESTRATION(7,1)\|PLUGGING ABANDONED BOREHOLE(7,1)\|INNER WALL(6,9)\|WELLBORE(6,5)\|ARGILLACEOUS CONTENT(6,2)\|CIRCUMFERENTIAL SURFACE(6,2)\|LIME MILK TURBID LIQUID(6,2)\|WELL ANNULAR CEMENT(6,2)\|MAXIMUM SPEED LIMIT(6,1)\|WELL MOUTH(6,1)\|WELLHEAD GAS FLOWMETER(6,1)\|WELLHEAD VENT VALVE(6,1)\|ABANDONED DRILLED WELL(5,4)\|CARBON DIOXIDE STORAGE RESERVOIR(5,4)\|ABANDONED WELL LOGGING INFORMATION(5,2)\|CARBON NEUTRALIZATION(5,2)\|FINE CRACK(5,2)\|FORMATION PERMEABILITY(5,2)\|PACKER DISTANCE(5,2)\|STIRRING BOX(5,2)\|COMPACT WHOLE FIRMNESS(5,1)\|FORMATION TEMPERATURE2THE SOLUBILITY(5,1)\|OVERLYING STRATUM(5,1)\|PROJECT DEMONSTRATION(5,1)\|VOLCANIC ASH CEMENT(5,1)\|WELL DRILLING(4,6)\|LAYER PROTECTION(4,3)\|WELL SEALING(4,2)\|ABANDONED DRILLING(4,1)\|CRACK PORT(4,1)\|FRACTURE LEAKAGE(4,1)\|GEOLOGICAL SEALING(4,1)\|LIME MILK SUSPENSION REACTION(4,1)\|PERFORATION INTERVAL(4,1)\|PERFORATION ZONE(4,1)\|PERMEABILITY CALCULATION(4,1)\|REPAIR DIFFICULTY(4,1)\|WELLHEAD PERIMETER CARBON DIOXIDE(4,1)\|INJECTION TERMINATION SET PRESSURE(3,4)\|CONTINUITY(3,2)\|SET INJECTION TERMINATION PRESSURE(3,2)\|BLOWOUT PREVENTER COMPONENT(3,1)\|CARBON DIOXIDE LEAKAGE PLUGGING(3,1)\|CARBON DIOXIDE RESERVOIR0AND(3,1)\|CONJECTURE(3,1)\|FOSSIL ENERGY(3,1)\|IDENTIFYING LEAKAGE(3,1)\|LEAKAGE REASON(3,1)\|	(CN113494265)\|1. A plugging method for leakage along an abandoned well in a carbon dioxide geological storage process is characterized by comprising the following steps of: the method comprises the following steps:\|step 1: perforating, namely perforating a perforating section formed on the inner wall of the shaft corresponding to the thickness of the stable covering layer, and communicating the annular cement of the drilling well with cracks of the surrounding rock breaking zone;\|step 2: injecting lime milk suspension, namely injecting the lime milk suspension into the perforation, so that the lime milk suspension enters the crack and reacts with leaked carbon dioxide to form calcium carbonate, and further plugging a leakage channel of the carbon dioxide;\|the plugging method further comprises at least one of the following steps:\|prior to step 1, comprising:\|a leakage identification step of identifying whether or not the abandoned well has carbon dioxide leaked along the well; and/or the number of the groups of groups,\|cleaning the inside of the well, namely cleaning a sealing bridge plug in the well before sealing the leaked abandoned well, and ensuring the smoothness and smoothness of the inner wall of the well shaft above the carbon dioxide geological sealing storage layer;\|and/or the number of the groups of groups,\|after step 2, it includes:\|a plugging effect monitoring step, namely monitoring the plugging effect of the well drilling after plugging; and/or, well sealing, namely, sealing the well by an in-well bridge plug for the well drilling after the well is plugged;\|in the step (1) of the process,\|before perforation, a relatively closed space is arranged in the well corresponding to the cover layer part, and the perforation section is arranged in the space; and/or the number of the groups of groups,\|in the step 2 of the process, the process is carried out,\|injecting lime milk suspension through a fracturing truck; and/or when injection begins, the injection pressure P is less than the reservoir pressure P 0 When the concentration of the lime milk suspension is an initial set concentration, and when P is larger than P 0 When the concentration of the lime milk suspension is reduced at a threshold value, the lime milk suspension is continuously injected, and when P is larger than P again 0 And when the threshold value is reached, the concentration of the lime milk suspension is reduced again, then the injection is continued until the concentration of the lime milk suspension is equal to a final set concentration, namely, the injection is continued at the final set concentration until the injection pressure P reaches an injection termination set pressure, and the injection is ended.\|2. The plugging method of claim 1, wherein:\|in the step (1) of the process,\|the aperture of the perforation is controlled to be 5-20 mm; and/or the number of the groups of groups,\|the density of perforation is 10 holes/m-30 holes/m; and/or the number of the groups of groups,\|the depth of perforation is preferably that the drilling annular cement and surrounding rock fracture zone are penetrated; and/or the number of the groups of groups,\|the ratio of the height of the perforation section to the height of the cover layer is 0.1-0.9; and/or the number of the groups of groups,\|the height of the perforating section is between 5 and 30 meters; and/or the number of the groups of groups,\|the distance between the upper edge of the perforation section and the upper edge of the cover layer is more than 5 meters; and/or the number of the groups of groups,\|the spacing between the lower edge of the perforation section and the lower edge of the cap layer is > 5 meters; and/or the number of the groups of groups,\|the perforation sections are uniformly distributed on the whole circumferential surface of the inner wall of the well; and/or the number of the groups of groups,\|the method of determining the position and thickness of the cap layer is at least one of the following:\|(1) Determining the position and thickness of a stable covering layer by analyzing logging and logging data of the abandoned drilling well in the drilling well;\|(2) The location and thickness of the overburden is determined by sonic logging of the abandoned borehole.\|3. The plugging method of claim 1, wherein: the measures for setting the space are as follows: installing an upper packer and a lower packer, wherein the two packers separate carbon dioxide stored in a reservoir layer below the cover layer for storing carbon dioxide and water in an overlying stratum above the cover layer; an injection pipe is arranged on the upper packer, and the pipe orifice at the upper end of the injection pipe is connected with a lime milk suspension injection device arranged on the wellhead, so that lime milk suspension is input into the closed space through the injection pipe and then is injected into the perforation; and/or the number of the groups of groups,\|the threshold value of the difference between the injection pressure P and the reservoir pressure is related to at least one of the following factors:\|(1) The thickness of the cap layer or the thickness of the cap layer and its permeability;\|(2) The permeability of the drilling annulus cement sheath; and/or the number of the groups of groups,\|the threshold is 0.5MPa; and/or the number of the groups of groups,\|the injection pressure is the pressure at the perforation section; and/or the number of the groups of groups,\|the injection termination setting pressure is 1.0MPa; and/or the number of the groups of groups,\|initial set concentration of injected lime milk suspension and injection pressure P and reservoir pressure P of carbon dioxide reservoir 0 Correlation; and/or the number of the groups of groups,\|the initial set concentration of the lime milk suspension is 2-10 mol/L; and/or the number of the groups of groups,\|the injection speed of the lime milk suspension is not higher than 0.5L/s; and/or the number of the groups of groups,\|in the process of injecting lime milk suspension, the injection speed is unchanged; and/or the number of the groups of groups,\|whenever injection pressure P and reservoir pressure P 0 When the difference reaches the threshold value, reducing the multiple of the concentration of the lime milk suspension to be a constant value; and/or the number of the groups of groups,\|the final set concentration is Ca (HO) 2 Solubility at carbon dioxide reservoir temperature.\|4. The plugging method according to claim 3, wherein: in the installation of the packer(s),\|the distance between the packer and the perforating section is more than 2.5 meters; and/or the number of the groups of groups,\|the distance between the packer on the upper part and the upper edge of the cover layer is more than 2.5 meters; and/or the number of the groups of groups,\|the distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters.\|5. The plugging method according to claim 2, wherein: the depth of the perforations is not less than 30 cm.\|6. The plugging method according to claim 3, wherein: the constant value that reduces the multiple of the lime milk suspension concentration is 0.2.\|7. The plugging method of claim 1, wherein: the initial set concentration of the lime milk suspension is 2-10mol/L, when the injection pressure P is greater than the reservoir pressure P 0 And P 0 The pressure difference of (2) exceeds the threshold value by 0.5MPa, the concentration of the lime milk suspension is reduced by 0.2 times of the initial set concentration value, at the moment, the injection pressure P is reduced to ensure that the pressure difference is lower than the threshold value, and the injection pressure is increased as the injection is continued to ensure that the P and the P are formed 0 When the difference of (2) exceeds 0.5MPa again,the concentration of the lime milk suspension is reduced to be 0.2 times of the previous concentration value again, and the process is repeated until the concentration of the lime milk suspension is lower than the solubility of calcium hydroxide at the formation temperature, then the saturated solution of lime milk with the solubility as the concentration enables the injection to be carried out again, the injection pressure is gradually increased, and when P and P are reached 0 When the difference of the two is 1.0MPa, the injection plugging process is finished.\|8. The plugging method of claim 1, wherein:\|in the step of identifying the leak, the leak is identified,\|monitoring the abandoned well for carbon dioxide leakage by at least one of:\|(1) Monitoring the leakage amount of the carbon dioxide at the wellhead;\|(2) Monitoring the wellhead perimeter carbon dioxide concentration to determine a leakage path of carbon dioxide along the abandoned borehole; and/or the number of the groups of groups,\|in the leakage identification step, a blowout prevention protection device is arranged at a wellhead, and an exhaust valve is arranged on the protection device; and/or the number of the groups of groups,\|in the step of cleaning in the well, cleaning a plugging bridge plug in the well shaft through a drilling machine; and/or the number of the groups of groups,\|in the plugging effect monitoring step, at least one of the following measures is taken:\|(1) A monitoring well is drilled beside the abandoned well, the monitoring well is deep above the cover layer, a pH value probe is arranged in the monitoring well, and the leakage condition of carbon dioxide is monitored by monitoring the pH value of formation water;\|(2) Monitoring the amount of leakage of carbon dioxide from the wellhead and/or the periphery of the wellhead of the well; and/or the number of the groups of groups,\|the monitoring frequency is: not less than once every 12 hours; and/or the number of the groups of groups,\|the monitoring period is as follows: after 30 days, no carbon dioxide leakage is found within 30 days, and the good plugging effect is proved; and/or the number of the groups of groups,\|injecting carbon dioxide corrosion resistant cement into the perforation section in the well to form an anti-leakage bridge plug in the well; and/or the number of the groups of groups,\|at least the upper packer is removed prior to cement injection.\|9. The plugging method of claim 8, wherein: the carbon dioxide corrosion resistant cement is: slag cement, pozzolan cement, fly ash cement or composite cement.	(CN113494265)\|TECHNICAL FIELD\|[0001] The invention belongs to the field of geological sealing of greenhouse gases, and relates to a sealing method for leakage along an abandoned well in the geological sealing process of carbon dioxide.\|BACKGROUND ART\|[0002] Carbon dioxide geological sequestration is a carbon dioxide emission reduction technique that injects and permanently sequesters carbon dioxide into geologic bodies such as underground aquifers or abandoned hydrocarbon reservoirs. The method is an emerging carbon dioxide treatment technology with large-scale application potential, and provides a possibility for near zero emission of carbon dioxide used for fossil energy.\|[0003] The government of China has paid great attention to and actively coped with climate change, and has put forward a ' carbon dioxide emission strives to reach a peak before 2030 and strives to achieve a ' ambitious goal of carbon neutralization before 2060 '. To achieve the aim of carbon neutralization, the carbon capturing and sealing technology is the final bottom technology after the maximum emission reduction aim is achieved in industries such as industry, transportation, construction and the like in China. At present, great project demonstration of carbon capture utilization and sealing is developed in each industry of China, and a foundation is laid for subsequent large-scale carbon dioxide injection.\|[0004] Carbon dioxide injected into a reservoir can leak through abandoned borehole, fault or overburden weaknesses due to uncertainty caused by field geological conditions and human development activities, while carbon dioxide leaks along the borehole generally because of chemical or mechanical effects causing carbon dioxide to leak along the borehole annulus cement, wellbore bridge plugs or surrounding rock fracture zones. The current situation is unfavorable for coping with the problem of sudden leakage along abandoned drilling in the carbon dioxide geological sealing process, and the development of the important environmental protection project of underground carbon dioxide sealing is limited to a great extent.\|DISCLOSURE\|Disclosure of Invention\|[0005] The invention aims to solve the problem of leakage of underground carbon dioxide from abandoned wells in the prior art, and provides a method for plugging leakage along abandoned wells in the geological carbon dioxide plugging process.\|[0006] The technical scheme adopted for achieving the purposes of the invention is as follows:\|[0007] a method of plugging leaks along abandoned wells during geological sequestration of carbon dioxide, comprising the steps of:\|[0008] step 1: perforating, namely perforating on the inner wall of the shaft corresponding to the thickness of the stable covering layer, and communicating the annular cement of the drilling well with cracks of the surrounding rock breaking zone;\|[0009] step 2: and injecting lime milk suspension, namely injecting the lime milk suspension into the perforation, so that the lime milk suspension enters the crack and reacts with the leaked carbon dioxide to form calcium carbonate, and further plugging a leakage channel of the carbon dioxide.\|[0010] Preferably, the method comprises the steps of,\|[0011] the plugging method further comprises at least one of the following steps:\|[0012] prior to step 1, it may comprise:\|[0013] and a leakage identification step of identifying whether the abandoned drilling well has carbon dioxide leaked along the drilling well.\|[0014] And cleaning the inside of the well, namely cleaning the sealing bridge plug in the well before sealing the leaked abandoned well, and ensuring the smoothness and smoothness of the inner wall of the well shaft above the carbon dioxide geological sealing storage layer.\|[0015] After step 2, it may include:\|[0016] and a plugging effect monitoring step, namely monitoring the plugging effect of the well drilling after plugging.\|[0017] And (3) well sealing, namely, performing in-well bridge plug well sealing on the well drilling after well sealing.\|[0018] In step 1, the process is preferably performed,\|[0019] a relatively closed space is provided in the wellbore corresponding to the cap layer prior to perforation, in which space the perforated section is disposed.\|[0020] Specifically, installing an upper packer and a lower packer in a well bore, wherein the two packers isolate carbon dioxide sealed in a reservoir in the well bore from water in an overlying stratum; an injection pipe is arranged on the upper packer, and lime cream suspension is input into the closed space through the injection pipe and then is injected into the perforation.\|[0021] In the installation of the packer(s),\|[0022] the distance of the packer from the perforation section is preferably greater than 2.5 meters.\|[0023] The distance of the packer in the upper part from the upper edge of the cover layer is > 2.5 meters.\|[0024] The distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters.\|[0025] Preferably, in said step 1, the step of, in the step of,\|[0026] the aperture of the perforation is controlled to be 5-20 mm.\|[0027] The density of perforations is 10-30 holes/m.\|[0028] The depth of perforation is preferably not less than 30 cm, preferably penetrating the drilling annulus cement and surrounding rock fracture zone.\|[0029] The ratio of the height of the perforation section to the height of the cap layer is 0.1-0.9. The height of the perforation section is preferably between 5 and 30 meters.\|[0030] The spacing between the upper edge of the perforation section and the upper edge of the cap layer is > 5 meters.\|[0031] The spacing between the lower edge of the perforation section and the lower edge of the cap layer is > 5 meters.\|[0032] The perforation sections are uniformly distributed on the whole circumferential surface of the inner wall of the well.\|[0033] In the step 1, the cover layer is referred to as a stable cover layer, which is a protective layer on the carbon dioxide geological sealing storage layer, and can seal the carbon dioxide in the storage layer to prevent the carbon dioxide from escaping upwards, and has the characteristics of high mud content, good continuity, large thickness and the like.\|[0034] The position and thickness of the cap layer are to be determined, and the method of determining the cap layer may be at least one of the following methods:\|[0035] (1) Determining the position and thickness of a stable covering layer by analyzing logging and logging data of the abandoned drilling well in the drilling well;\|[0036] (2) The location and thickness of the overburden is determined by sonic logging of the abandoned borehole.\|[0037] In step 2, preferably, the lime milk suspension is injected by means of a fracturing truck.\|[0038] Initial concentration of injected lime milk suspension and injection pressure P and reservoir pressure P of carbon dioxide reservoir 0 And (5) correlation.\|[0039] When injection begins, the injection pressure P is less than the reservoir pressure P 0 When the concentration of the lime milk suspension is an initial set concentration, and when P is larger than P 0 When the concentration of the lime milk suspension is reduced at a threshold value, the lime milk suspension is continuously injected, and when P is larger than P again 0 And when the threshold value is reached, the concentration of the lime milk suspension is reduced again, then the injection is continued until the concentration of the lime milk suspension is equal to a final set concentration, namely, the injection is continued again with the final set concentration until the injection pressure P reaches an injection termination set pressure, and the injection is ended.\|[0040] Preferably, the method comprises the steps of,\|[0041] the threshold value of the difference between the injection pressure P and the reservoir pressure is related to at least one of the following factors:\|[0042] (1) The thickness of the cap layer or the thickness of the cap layer and its permeability;\|[0043] (2) The permeability of the annulus cement sheath.\|[0044] Preferably, the threshold is 0.5MPa.\|[0045] The injection pressure is the pressure at the perforation section. I.e. the pressure of the enclosed space between the two packers.\|[0046] The injection termination setting pressure is preferably 1.0MPa.\|[0047] Preferably, the initial set concentration of the lime milk suspension is 2-10 mol/liter.\|[0048] Preferably, the injection rate of the lime milk suspension is not higher than 0.5L/s.\|[0049] Preferably, the injection rate is constant during the injection of the lime milk suspension.\|[0050] When the difference between the injection pressure P and the reservoir pressure reaches the threshold value, the multiple of the concentration of the lime milk suspension is reduced to a constant value. Preferably, the constant value is 0.2.\|[0051] The final set concentration is Ca (HO) 2 Solubility at carbon dioxide reservoir temperature.\|[0052] One preferable scheme is as follows: the initial set concentration of the lime milk suspension is 2-10mol/L, when the injection pressure P is greater than the reservoir pressure P 0 And P 0 The pressure difference of (2) exceeds the threshold value by 0.5MPa, the concentration of the lime milk suspension is reduced by 0.2 times of the initial set concentration value, at the moment, the injection pressure P is reduced to ensure that the pressure difference is lower than the threshold value, and the injection pressure is increased as the injection is continued to ensure that the P and the P are formed 0 When the difference value of the concentration of the lime milk suspension exceeds 0.5MPa again, the concentration of the lime milk suspension is reduced to be 0.2 times of the previous concentration value, and the process is repeated circularly until the concentration of the lime milk suspension is lower than the solubility of calcium hydroxide at the formation temperature, then the solubility is used as the concentration of lime milk to be injected, the injection is continued again, the injection pressure is gradually increased, and when P and P are equal to each other 0 When the difference of the two is 1.0MPa, the injection plugging process is finished.\|[0053] Formation temperature may be found from well log and log data of the well, and may also be obtained by methods inferred in the art.\|[0054] In the leak identification step, the leak identification step is preferably,\|[0055] monitoring the abandoned well for carbon dioxide leakage by at least one of:\|[0056] (1) Monitoring the leakage amount of the carbon dioxide at the wellhead;\|[0057] (2) The wellhead perimeter carbon dioxide concentration is monitored to determine the path of leakage of carbon dioxide along the abandoned borehole.\|[0058] Preferably, in the leak identification step, a blowout prevention protection device is provided at the wellhead, and an exhaust valve is provided on the protection device.\|[0059] And closing the exhaust valve when monitoring the carbon dioxide concentration around the wellhead.\|[0060] In the well cleaning step, the plugging bridge plugs in the wellbore are preferably cleaned by a drilling rig.\|[0061] In the plugging effect monitoring step, the plugging effect is preferably,\|[0062] at least one of the following measures is taken:\|[0063] (1) A monitoring well is drilled beside the abandoned well, the monitoring well is deep above the cover layer, a pH value probe is arranged in the monitoring well, and the leakage condition of carbon dioxide is monitored by monitoring the pH value of formation water;\|[0064] (2) The amount of leakage of carbon dioxide from the wellhead and/or the periphery of the wellhead of the well is monitored.\|[0065] Preferably, the method comprises the steps of,\|[0066] the monitoring frequency is: not less than once every 12 hours.\|[0067] The monitoring period is 30 days, and no carbon dioxide leakage is found within 30 days, so that the plugging effect is proved to be good.\|[0068] In the well-sealing step, the well is preferably,\|[0069] and injecting carbon dioxide corrosion resistant cement into the perforation section in the well to form the leakage-proof bridge plug in the well.\|[0070] The upper packer is removed prior to cement injection. The lower packer may be left in the well.\|[0071] The carbon dioxide corrosion resistant cement is preferably: slag cement, pozzolan cement, fly ash cement, composite cement, and the like.\|[0072] The plugging method for plugging leakage along the abandoned well in the geological carbon dioxide plugging process solves the problem of leakage of carbon dioxide from annular cement around abandoned wells and cracks of surrounding rock fracture zones in the carbon dioxide plugging process in the background technology, selects a cover layer with good stratum sealing performance for perforation, communicates a shaft with leakage risk, well annular cement and surrounding rock fracture zones, and can be used for plugging a carbon dioxide leakage channel by injecting lime milk suspension into a perforation section to enable lime milk entering a gap to react with leaked carbon dioxide to form hardened compact calcium carbonate, and simultaneously cementing the surrounding rock fracture zones and the crack-containing well annular cement into a compact whole, thereby greatly reducing the leakage risk along the abandoned well in the geological carbon dioxide plugging process. The invention has the beneficial effects based on the technical scheme that:\|[0073] (1) According to the plugging method, the stable cover layer on the carbon dioxide geological storage layer is preferably used for perforating and plugging the cracks, so that the crack channels leaked along the abandoned well in the carbon dioxide geological storage process can be effectively plugged.\|[0074] (2) According to the plugging method, the lime milk suspension is used for plugging the cracks, hardened and compact calcium carbonate can be generated by the reaction of the lime milk and leaked carbon dioxide in the cracks, a carbon dioxide leakage channel can be effectively plugged, and the formed calcium carbonate can be kept stable under the condition of no external disturbance.\|[0075] (3) According to the plugging method, the concentration of the lime milk suspension injected into the cracks is from high to low, the lime milk suspension with low concentration is more beneficial to entering the fine cracks, and calcium carbonate formed by the reaction of the lime milk suspension and carbon dioxide has a better plugging effect on the cracks.\|[0076] (4) According to the plugging method, lime milk suspension is injected into cracks to react with carbon dioxide to form compact calcium carbonate, and the process can bond a surrounding rock breaking zone and crack-containing drilling annular cement into a compact whole, so that the risk of leakage along an abandoned well in the geological carbon dioxide plugging process is greatly reduced.\|[0077] (5) According to the plugging method, the injected lime milk suspension reacts with the carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, so that the risk of geological environment pollution is extremely low, and the plugging process is safe and environment-friendly.\|[0078] The invention is illustrated in detail below by means of the figures and examples.\|DRAWINGS DESCRIPTION\|[0079] FIG. 1 is a schematic illustration of a plugging process for carbon dioxide leakage along a abandoned well in the present invention.\|[0080] FIG. 2 is a flow chart of the plugging of carbon dioxide leaks along a abandoned well in the present invention.\|INVENTION MODE\|Detailed Description\|[0081] The present invention is described in detail below with reference to fig. 1 and the embodiment. Fig. 1 shows a facility, an arranged plugging structure and equipment for plugging abandoned wells by the plugging method provided by the invention. The plugging method is illustrated by fig. 2.\|[0082] The method comprises the following specific steps of:\|[0083] step 1: identifying leakage;\|[0084] step 2: cleaning in a well;\|[0085] step 3: perforating;\|[0086] step 4: plugging;\|[0087] step 5: monitoring plugging effect;\|[0088] step 6: and (5) sealing the well.\|[0089] The following is a detailed description.\|[0090] Firstly, a leakage identification step is carried out on abandoned wells to find out the leakage position and the leakage amount of carbon dioxide along the abandoned wells, a simple bracket can be arranged at a wellhead, and a gas flowmeter 16 is supported at the wellhead to determine whether the wellhead emits carbon dioxide or not. If a carbon dioxide leak is detected, i.e. the plugging method of the invention is ready to be carried out, the blowout preventer 1 is first installed at the wellhead, and the gas flow meter 16 is a component of the blowout preventer and is arranged on the protector, as shown in fig. 1.\|[0091] The blowout prevention protection device is installed in order to prevent the risk of leakage of a large amount of gas existing after perforation.\|[0092] Another measure of leak identification is: closing an exhaust valve on the blowout preventer, and monitoring the concentration of carbon dioxide at the wellhead perimeter to determine the path of leakage of carbon dioxide along the abandoned wellbore. Judging whether the carbon dioxide leaks through the cracks of the annular cement and the surrounding rock fracture zone of the well drilling or leaks from other parts of the weak cap layer, and if the carbon dioxide leaks from other positions, taking other measures to perform plugging is not the content of the invention and is not repeated herein.\|[0093] And then, carrying out an in-well cleaning step on the well shaft 2, cleaning a cement bridge plug in the well shaft 2 by adopting a drilling machine, and selecting and determining the position and the thickness of the stable cover layer 3 with good stratum sealing performance.\|[0094] The selection of a stable cap layer can be performed by analyzing well logging and logging information, and the position and thickness of the cap layer can be determined by means of sonic detection.\|[0095] The stable cover layer is a protective layer which is arranged on the carbon dioxide geological seal storage layer 9 and can seal the carbon dioxide in the storage layer 9 from upward dissipation, has the characteristics of high clay content, good continuity, large thickness and the like, and the porosity of the cover layer 3 is generally less than 5 percent, and the permeability is less than 1mD.\|[0096] Then, perforating 4 is carried out on the inner wall of the corresponding cover layer 3 of the shaft 2, and the perforating 4 is communicated with the cracks 7 of the drilling annular cement 5 and the surrounding rock breaking belt 6;\|[0097] when drilling is excavated, after the shaft 2 passes through the cover layer 3, the cover layer around the shaft 2 is damaged, annular cement 5 and surrounding rock breaking zones 6 are formed around the shaft 2, and cracks 7 are large, so that carbon dioxide in a reservoir layer leaks out through the cracks 7. The plugging method of the invention is to plug the leakage.\|[0098] A relatively closed space is required in the wellbore 2 at the perforation interval at the corresponding cap prior to perforation to avoid the risk of significant amounts of carbon dioxide and water entering the wellbore 2 during perforation. The measures for setting the closed space are as follows: installing an upper packer 8 and a lower packer 8 on the inner wall of the well shaft corresponding to the cover layer 3 in the well shaft 2, wherein the two packers 8 isolate carbon dioxide sealed in a reservoir 9 below the cover layer 3 from water in an overburden stratum 10 above the cover layer; an injection pipe, also called a central pipe 18, is arranged on the upper packer 8, the upper pipe orifice of the central pipe 18 is connected with a lime milk suspension injection device fracturing truck 12 arranged on the wellhead, the fracturing truck 12 is connected with a stirring box, and lime milk suspension with required concentration is provided, so that the lime milk suspension is input into the closed space through the injection pipe at a certain speed, and then is injected into the perforation.\|[0099] Preferably, the distance of the packer from the perforation section during the step of setting the packer is greater than 2.5m. The distance of the packer in the upper part from the upper edge of the cover layer is > 2.5 meters. The distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters. The aperture of the perforations 4 is controlled to be 5-20mm, in this embodiment, for example, 7mm. The density of perforations is 10 holes/meter-30 holes/meter, in this embodiment, 20 holes/meter in the perforation section. The ratio of the height of the perforating section to the height of the cover layer is 0.1-0.9, the ratio value is selected in relation to the thickness of the cover layer, the thickness of the cover layer is generally tens of meters to hundreds of meters, when the thickness of the cover layer is thinner, the ratio value is slightly larger, and when the thickness of the cover layer is thicker, the ratio value is slightly smaller, so that the height of the perforating section is ensured to be more suitable for 5-30 meters. Preferably, the spacing between the upper and lower edges of the perforation section and the upper and lower edges of the cap layer is greater than 5 meters. In this embodiment, both pitches are, for example, 8 meters.\|[0100] According to the invention, lime milk is injected into the perforation of the cover layer, and on annular cement and surrounding rock fracture zones where cracks appear due to the damage of drilling on the cover layer, the lime milk and carbon dioxide meet and react in the cracks to generate calcium carbonate to fill and seal the cracks, so that the cover layer is repaired. Therefore, the aperture and density of the perforation can influence the state that the lime milk suspension enters the cracks, if the aperture of the perforation is too small, the flow of the lime milk can be blocked, so that the contact between the lime milk and the carbon dioxide is poor, but if the aperture is too large, the cover layer can be damaged greatly, the repairing difficulty is increased, and the distribution of the lime milk in the drilling annulus cement 5 and the surrounding rock breaking zone 6 can be influenced by the density of the perforation. The proper aperture and density of the perforation are selected, and the position and the height of the perforation section in the cover layer can influence the stability and the firmness of cementing the surrounding rock breaking zone and the annular cement of the fractured well into a compact whole and the high efficiency of plugging construction.\|[0101] It is also a good measure that the perforation segments are evenly distributed over the entire circumference of the inner wall of the well. Because the crack position is not well controlled, the position where the crack possibly appears can be fully covered by the uniform perforation, and a better plugging effect can be obtained.\|[0102] The next step is to perform the plugging by injecting a lime milk suspension into the enclosed space, i.e. into the perforations 4. Preparing lime milk suspension (Ca (HO) with initial set concentration not less than 2mol/L (2-10 mol/L) by using a stirring box 11 arranged on a wellhead 2 Colloidal solution), for example, an initial set concentration of 5mol/L, is slowly injected into the perforation section by means of the fracturing unit 12 through the central conduit 18 at a rate of less than 0.5L/s, for example, 0.3L/s, when the injection pressure P is higher than the reservoir pressure P 0 A threshold value, for example, 0.5MPa, which is a value of 0.2 times the initial injection concentration, i.e., the concentration is reduced to 1mol/L, and then the injection is continued slowly at a rate of 0.3L/s, and when the injection pressure P is raised again by a threshold value of 0.5MPa, the concentration of the lime milk suspension is reduced again to 0.2 times the previous concentration, i.e., the concentration is reduced to 0.2mol/L, and the injection is continued, and the cycle is continued until the lime milk concentration is equal to or less than the formation temperature, i.e., the temperature of the carbon dioxide reservoir 9, ca (HO 2 For example, the temperature of reservoir 9 is 60 ℃, ca (HO) at this time 2 The solubility of (C) was 0.02mol/L. Thus, when the injection pressure is increased by two more thresholds, the concentration of milk of lime is reduced to Ca (HO) at the formation temperature 2 Is a solvent for the polymer. At this time, the injection was continued at a concentration of 0.02mol/L, the concentration of lime milk was not lowered any more, and the above-mentioned solubility was the final set concentration. Continuing the injection at this final set concentration, the injection pressure gradually increases and, when increasing to an injection termination set pressure, the injection ends. This injection termination set pressure was 1.0MPa.\|[0103] As another example, where the initial set concentration of milk of lime is 10mol/L, the threshold value is also 0.5MPa when the injection pressure P reaches a value higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 2mol/L, the injection is continued, and when the injection pressure P is higher than the reservoir pressure P again 0 At 0.5MPa, the concentration is reduced to 0.4 mol/L again, the injection is continued, and the third injection pressure is higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 0.08 mol/L, and the fourth injection pressure is higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 0.016 mol/L, which is lower than the solution degree of 0.02mol/L, and at this time, the solution is injected at the final set concentration, namely the solubility, until the injection pressure is 1.0MPa.\|[0104] The pressure difference of the threshold value and the thickness of the cement sheath can calculate the stratum permeability, and when the parameters are set, the calculated stratum permeability of the cement sheath is close to the stratum permeability of the cover layer, and the closed crack under the lime milk concentration condition can be considered to be not leaked. The fact that a threshold value is reached indicates that the lime milk with the existing concentration is not easy to continue to be injected, so that the concentration needs to be reduced, the concentration is reduced by a constant multiple, the operation is facilitated, and more importantly, the completion of plugging of fine cracks can be achieved gradually.\|[0105] In the injection process, the concentration of lime milk is adjusted, and initially, the concentration is larger, larger cracks are filled as soon as possible, then the concentration is reduced, lime milk with lower concentration easily enters smaller cracks, and fine cracks can be plugged. At the initial set concentration, the plugging can be completed within 10 times of concentration reduction according to the rate reduction of 0.2 times, and the setting is ideal. If the initial set concentration is too low, an integral structure with good plugging performance is not easy to form. However, if the initial set concentration is too high, the lime milk is too thick, and besides the problems of the above and the increase of the concentration reduction times, ports of some cracks are sealed by the thick lime milk, so that the whole annular cement and the size cracks in the surrounding rock breaking zone are not filled, and the sealing effect is also affected.\|[0106] The lowest final set concentration of milk of lime is not lower than the solubility at the temperature of the reservoir 9, which serves to let the milk of lime suspension sufficiently enter the fissures 7 at a set final set pressure (e.g. 1.0 MPa). But the final set concentration must not be below the solution level, otherwise, the subsequent injection of unsaturated lime water will have a damaging effect on the calcium carbonate formed by the reaction of the previously injected lime milk with carbon dioxide.\|[0107] The injection rate described above also affects the occlusion effect. The invention provides a maximum rate limit of 0.5 liter/second at which lime milk entering the crack can react with leaked carbon dioxide in good time to form calcium carbonate to seal the crack. If the speed limit is too high, the blocking effect is not good, but if the speed limit is too low, the blocking is not easy to proceed and the blocking efficiency is too low.\|[0108] The plugging effect monitoring step follows.\|[0109] Monitoring can also be performed by using a gas flow meter provided at the wellhead to measure the gas flow at the wellhead. A wellhead vent valve, which is a valve to a gas flow meter, may also be closed, and the wellhead perimeter carbon dioxide concentration monitored to determine the leak path of carbon dioxide along the abandoned borehole.\|[0110] Alternatively, a monitoring well 13 may be drilled on the side of the well, the well depth of which does not exceed the cap layer 3.\|[0111] Ph value probes (14), an earth surface carbon dioxide concentration meter (15) and a wellhead gas flowmeter (16) are placed in a monitoring well (13) to be matched for use, the Ph value of overlying stratum water, the wellhead periphery carbon dioxide concentration and wellhead carbon dioxide leakage are continuously monitored, and data are analyzed through an earth surface monitoring station (17).\|[0112] The frequency of monitoring may be generally such that data is taken every 12 hours.\|[0113] If no carbon dioxide leakage is found in the 30-day monitoring, the plugging is considered to be successful, and then the following process steps are carried out: and (5) sealing the well.\|[0114] The bridge plug well sealing in the well can be implemented, and the sealing of the leakage of the carbon dioxide along the abandoned well is completed.\|[0115] Firstly, taking out the packer at the upper part of the perforation section, injecting carbon dioxide corrosion resistant cement and the like into the perforation section in the well to form a cement bridge plug for preventing leakage in the well, and integrally completing the plugging of the leakage of carbon dioxide along the abandoned well. The carbon dioxide corrosion resistant cement can be slag cement, volcanic ash cement, fly ash cement or composite cement, etc., and the concrete method of well sealing belongs to the prior art and is not repeated here.\|[0116] If the sealing is not up to standard through monitoring, the leakage reason needs to be specifically analyzed, if the leakage is still caused by the crack around the drilling well, the perforation 4 can be set at a new position again, lime milk can be refilled, at this time, the concentration of the lime milk can be adjusted, for example, the set concentration is increased, and the lime milk can be refilled. And then monitoring the blocking effect until the blocking reaches the standard.\|[0117] According to the invention, the cover layer is preferably perforated, a shaft with leakage risk, drilling annulus cement and a surrounding rock breaking belt are communicated, a packer is arranged in the shaft, a relatively closed space is formed in a perforation section, lime milk suspension is slowly injected into the perforation section through a fracturing truck, the injection pressure is controlled in the process, the concentration of lime milk is gradually reduced, lime milk in a crack reacts with leaked carbon dioxide to form hardened and compact calcium carbonate, and a carbon dioxide leakage channel is further plugged. The invention can effectively block the crack channel leaked along the abandoned well in the geological carbon dioxide sealing process, and can bond the surrounding rock breaking zone and the crack-containing drilling annular cement into a compact whole, thereby greatly reducing the risk of leakage along the abandoned well in the geological carbon dioxide sealing process. The injected lime milk suspension reacts with the carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, so that the risk of geological environment pollution is extremely low, and the plugging process is safe and environment-friendly.	(CN113494265)\|TECHNICAL FIELD\|[0001] The invention belongs to the field of geological sealing of greenhouse gases, and relates to a sealing method for leakage along an abandoned well in the geological sealing process of carbon dioxide.\|BACKGROUND ART\|[0002] Carbon dioxide geological sequestration is a carbon dioxide emission reduction technique that injects and permanently sequesters carbon dioxide into geologic bodies such as underground aquifers or abandoned hydrocarbon reservoirs. The method is an emerging carbon dioxide treatment technology with large-scale application potential, and provides a possibility for near zero emission of carbon dioxide used for fossil energy.\|[0003] The government of China has paid great attention to and actively coped with climate change, and has put forward a ' carbon dioxide emission strives to reach a peak before 2030 and strives to achieve a ' ambitious goal of carbon neutralization before 2060 '. To achieve the aim of carbon neutralization, the carbon capturing and sealing technology is the final bottom technology after the maximum emission reduction aim is achieved in industries such as industry, transportation, construction and the like in China. At present, great project demonstration of carbon capture utilization and sealing is developed in each industry of China, and a foundation is laid for subsequent large-scale carbon dioxide injection.\|[0004] Carbon dioxide injected into a reservoir can leak through abandoned borehole, fault or overburden weaknesses due to uncertainty caused by field geological conditions and human development activities, while carbon dioxide leaks along the borehole generally because of chemical or mechanical effects causing carbon dioxide to leak along the borehole annulus cement, wellbore bridge plugs or surrounding rock fracture zones. The current situation is unfavorable for coping with the problem of sudden leakage along abandoned drilling in the carbon dioxide geological sealing process, and the development of the important environmental protection project of underground carbon dioxide sealing is limited to a great extent.\|DISCLOSURE\|Disclosure of Invention\|[0005] The invention aims to solve the problem of leakage of underground carbon dioxide from abandoned wells in the prior art, and provides a method for plugging leakage along abandoned wells in the geological carbon dioxide plugging process.\|[0006] The technical scheme adopted for achieving the purposes of the invention is as follows:\|[0007] a method of plugging leaks along abandoned wells during geological sequestration of carbon dioxide, comprising the steps of:\|[0008] step 1: perforating, namely perforating on the inner wall of the shaft corresponding to the thickness of the stable covering layer, and communicating the annular cement of the drilling well with cracks of the surrounding rock breaking zone;\|[0009] step 2: and injecting lime milk suspension, namely injecting the lime milk suspension into the perforation, so that the lime milk suspension enters the crack and reacts with the leaked carbon dioxide to form calcium carbonate, and further plugging a leakage channel of the carbon dioxide.\|[0010] Preferably, the method comprises the steps of,\|[0011] the plugging method further comprises at least one of the following steps:\|[0012] prior to step 1, it may comprise:\|[0013] and a leakage identification step of identifying whether the abandoned drilling well has carbon dioxide leaked along the drilling well.\|[0014] And cleaning the inside of the well, namely cleaning the sealing bridge plug in the well before sealing the leaked abandoned well, and ensuring the smoothness and smoothness of the inner wall of the well shaft above the carbon dioxide geological sealing storage layer.\|[0015] After step 2, it may include:\|[0016] and a plugging effect monitoring step, namely monitoring the plugging effect of the well drilling after plugging.\|[0017] And (3) well sealing, namely, performing in-well bridge plug well sealing on the well drilling after well sealing.\|[0018] In step 1, the process is preferably performed,\|[0019] a relatively closed space is provided in the wellbore corresponding to the cap layer prior to perforation, in which space the perforated section is disposed.\|[0020] Specifically, installing an upper packer and a lower packer in a well bore, wherein the two packers isolate carbon dioxide sealed in a reservoir in the well bore from water in an overlying stratum; an injection pipe is arranged on the upper packer, and lime cream suspension is input into the closed space through the injection pipe and then is injected into the perforation.\|[0021] In the installation of the packer(s),\|[0022] the distance of the packer from the perforation section is preferably greater than 2.5 meters.\|[0023] The distance of the packer in the upper part from the upper edge of the cover layer is > 2.5 meters.\|[0024] The distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters.\|[0025] Preferably, in said step 1, the step of, in the step of,\|[0026] the aperture of the perforation is controlled to be 5-20 mm.\|[0027] The density of perforations is 10-30 holes/m.\|[0028] The depth of perforation is preferably not less than 30 cm, preferably penetrating the drilling annulus cement and surrounding rock fracture zone.\|[0029] The ratio of the height of the perforation section to the height of the cap layer is 0.1-0.9. The height of the perforation section is preferably between 5 and 30 meters.\|[0030] The spacing between the upper edge of the perforation section and the upper edge of the cap layer is > 5 meters.\|[0031] The spacing between the lower edge of the perforation section and the lower edge of the cap layer is > 5 meters.\|[0032] The perforation sections are uniformly distributed on the whole circumferential surface of the inner wall of the well.\|[0033] In the step 1, the cover layer is referred to as a stable cover layer, which is a protective layer on the carbon dioxide geological sealing storage layer, and can seal the carbon dioxide in the storage layer to prevent the carbon dioxide from escaping upwards, and has the characteristics of high mud content, good continuity, large thickness and the like.\|[0034] The position and thickness of the cap layer are to be determined, and the method of determining the cap layer may be at least one of the following methods:\|[0035] (1) Determining the position and thickness of a stable covering layer by analyzing logging and logging data of the abandoned drilling well in the drilling well;\|[0036] (2) The location and thickness of the overburden is determined by sonic logging of the abandoned borehole.\|[0037] In step 2, preferably, the lime milk suspension is injected by means of a fracturing truck.\|[0038] Initial concentration of injected lime milk suspension and injection pressure P and reservoir pressure P of carbon dioxide reservoir 0 And (5) correlation.\|[0039] When injection begins, the injection pressure P is less than the reservoir pressure P 0 When the concentration of the lime milk suspension is an initial set concentration, and when P is larger than P 0 When the concentration of the lime milk suspension is reduced at a threshold value, the lime milk suspension is continuously injected, and when P is larger than P again 0 And when the threshold value is reached, the concentration of the lime milk suspension is reduced again, then the injection is continued until the concentration of the lime milk suspension is equal to a final set concentration, namely, the injection is continued again with the final set concentration until the injection pressure P reaches an injection termination set pressure, and the injection is ended.\|[0040] Preferably, the method comprises the steps of,\|[0041] the threshold value of the difference between the injection pressure P and the reservoir pressure is related to at least one of the following factors:\|[0042] (1) The thickness of the cap layer or the thickness of the cap layer and its permeability;\|[0043] (2) The permeability of the annulus cement sheath.\|[0044] Preferably, the threshold is 0.5MPa.\|[0045] The injection pressure is the pressure at the perforation section. I.e. the pressure of the enclosed space between the two packers.\|[0046] The injection termination setting pressure is preferably 1.0MPa.\|[0047] Preferably, the initial set concentration of the lime milk suspension is 2-10 mol/liter.\|[0048] Preferably, the injection rate of the lime milk suspension is not higher than 0.5L/s.\|[0049] Preferably, the injection rate is constant during the injection of the lime milk suspension.\|[0050] When the difference between the injection pressure P and the reservoir pressure reaches the threshold value, the multiple of the concentration of the lime milk suspension is reduced to a constant value. Preferably, the constant value is 0.2.\|[0051] The final set concentration is Ca (HO) 2 Solubility at carbon dioxide reservoir temperature.\|[0052] One preferable scheme is as follows: the initial set concentration of the lime milk suspension is 2-10mol/L, when the injection pressure P is greater than the reservoir pressure P 0 And P 0 The pressure difference of (2) exceeds the threshold value by 0.5MPa, the concentration of the lime milk suspension is reduced by 0.2 times of the initial set concentration value, at the moment, the injection pressure P is reduced to ensure that the pressure difference is lower than the threshold value, and the injection pressure is increased as the injection is continued to ensure that the P and the P are formed 0 When the difference value of the concentration of the lime milk suspension exceeds 0.5MPa again, the concentration of the lime milk suspension is reduced to be 0.2 times of the previous concentration value, and the process is repeated circularly until the concentration of the lime milk suspension is lower than the solubility of calcium hydroxide at the formation temperature, then the solubility is used as the concentration of lime milk to be injected, the injection is continued again, the injection pressure is gradually increased, and when P and P are equal to each other 0 When the difference of the two is 1.0MPa, the injection plugging process is finished.\|[0053] Formation temperature may be found from well log and log data of the well, and may also be obtained by methods inferred in the art.\|[0054] In the leak identification step, the leak identification step is preferably,\|[0055] monitoring the abandoned well for carbon dioxide leakage by at least one of:\|[0056] (1) Monitoring the leakage amount of the carbon dioxide at the wellhead;\|[0057] (2) The wellhead perimeter carbon dioxide concentration is monitored to determine the path of leakage of carbon dioxide along the abandoned borehole.\|[0058] Preferably, in the leak identification step, a blowout prevention protection device is provided at the wellhead, and an exhaust valve is provided on the protection device.\|[0059] And closing the exhaust valve when monitoring the carbon dioxide concentration around the wellhead.\|[0060] In the well cleaning step, the plugging bridge plugs in the wellbore are preferably cleaned by a drilling rig.\|[0061] In the plugging effect monitoring step, the plugging effect is preferably,\|[0062] at least one of the following measures is taken:\|[0063] (1) A monitoring well is drilled beside the abandoned well, the monitoring well is deep above the cover layer, a pH value probe is arranged in the monitoring well, and the leakage condition of carbon dioxide is monitored by monitoring the pH value of formation water;\|[0064] (2) The amount of leakage of carbon dioxide from the wellhead and/or the periphery of the wellhead of the well is monitored.\|[0065] Preferably, the method comprises the steps of,\|[0066] the monitoring frequency is: not less than once every 12 hours.\|[0067] The monitoring period is 30 days, and no carbon dioxide leakage is found within 30 days, so that the plugging effect is proved to be good.\|[0068] In the well-sealing step, the well is preferably,\|[0069] and injecting carbon dioxide corrosion resistant cement into the perforation section in the well to form the leakage-proof bridge plug in the well.\|[0070] The upper packer is removed prior to cement injection. The lower packer may be left in the well.\|[0071] The carbon dioxide corrosion resistant cement is preferably: slag cement, pozzolan cement, fly ash cement, composite cement, and the like.\|[0072] The plugging method for plugging leakage along the abandoned well in the geological carbon dioxide plugging process solves the problem of leakage of carbon dioxide from annular cement around abandoned wells and cracks of surrounding rock fracture zones in the carbon dioxide plugging process in the background technology, selects a cover layer with good stratum sealing performance for perforation, communicates a shaft with leakage risk, well annular cement and surrounding rock fracture zones, and can be used for plugging a carbon dioxide leakage channel by injecting lime milk suspension into a perforation section to enable lime milk entering a gap to react with leaked carbon dioxide to form hardened compact calcium carbonate, and simultaneously cementing the surrounding rock fracture zones and the crack-containing well annular cement into a compact whole, thereby greatly reducing the leakage risk along the abandoned well in the geological carbon dioxide plugging process. The invention has the beneficial effects based on the technical scheme that:\|[0073] (1) According to the plugging method, the stable cover layer on the carbon dioxide geological storage layer is preferably used for perforating and plugging the cracks, so that the crack channels leaked along the abandoned well in the carbon dioxide geological storage process can be effectively plugged.\|[0074] (2) According to the plugging method, the lime milk suspension is used for plugging the cracks, hardened and compact calcium carbonate can be generated by the reaction of the lime milk and leaked carbon dioxide in the cracks, a carbon dioxide leakage channel can be effectively plugged, and the formed calcium carbonate can be kept stable under the condition of no external disturbance.\|[0075] (3) According to the plugging method, the concentration of the lime milk suspension injected into the cracks is from high to low, the lime milk suspension with low concentration is more beneficial to entering the fine cracks, and calcium carbonate formed by the reaction of the lime milk suspension and carbon dioxide has a better plugging effect on the cracks.\|[0076] (4) According to the plugging method, lime milk suspension is injected into cracks to react with carbon dioxide to form compact calcium carbonate, and the process can bond a surrounding rock breaking zone and crack-containing drilling annular cement into a compact whole, so that the risk of leakage along an abandoned well in the geological carbon dioxide plugging process is greatly reduced.\|[0077] (5) According to the plugging method, the injected lime milk suspension reacts with the carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, so that the risk of geological environment pollution is extremely low, and the plugging process is safe and environment-friendly.\|[0078] The invention is illustrated in detail below by means of the figures and examples.\|DRAWINGS DESCRIPTION\|[0079] FIG. 1 is a schematic illustration of a plugging process for carbon dioxide leakage along a abandoned well in the present invention.\|[0080] FIG. 2 is a flow chart of the plugging of carbon dioxide leaks along a abandoned well in the present invention.\|INVENTION MODE\|Detailed Description\|[0081] The present invention is described in detail below with reference to fig. 1 and the embodiment. Fig. 1 shows a facility, an arranged plugging structure and equipment for plugging abandoned wells by the plugging method provided by the invention. The plugging method is illustrated by fig. 2.\|[0082] The method comprises the following specific steps of:\|[0083] step 1: identifying leakage;\|[0084] step 2: cleaning in a well;\|[0085] step 3: perforating;\|[0086] step 4: plugging;\|[0087] step 5: monitoring plugging effect;\|[0088] step 6: and (5) sealing the well.\|[0089] The following is a detailed description.\|[0090] Firstly, a leakage identification step is carried out on abandoned wells to find out the leakage position and the leakage amount of carbon dioxide along the abandoned wells, a simple bracket can be arranged at a wellhead, and a gas flowmeter 16 is supported at the wellhead to determine whether the wellhead emits carbon dioxide or not. If a carbon dioxide leak is detected, i.e. the plugging method of the invention is ready to be carried out, the blowout preventer 1 is first installed at the wellhead, and the gas flow meter 16 is a component of the blowout preventer and is arranged on the protector, as shown in fig. 1.\|[0091] The blowout prevention protection device is installed in order to prevent the risk of leakage of a large amount of gas existing after perforation.\|[0092] Another measure of leak identification is: closing an exhaust valve on the blowout preventer, and monitoring the concentration of carbon dioxide at the wellhead perimeter to determine the path of leakage of carbon dioxide along the abandoned wellbore. Judging whether the carbon dioxide leaks through the cracks of the annular cement and the surrounding rock fracture zone of the well drilling or leaks from other parts of the weak cap layer, and if the carbon dioxide leaks from other positions, taking other measures to perform plugging is not the content of the invention and is not repeated herein.\|[0093] And then, carrying out an in-well cleaning step on the well shaft 2, cleaning a cement bridge plug in the well shaft 2 by adopting a drilling machine, and selecting and determining the position and the thickness of the stable cover layer 3 with good stratum sealing performance.\|[0094] The selection of a stable cap layer can be performed by analyzing well logging and logging information, and the position and thickness of the cap layer can be determined by means of sonic detection.\|[0095] The stable cover layer is a protective layer which is arranged on the carbon dioxide geological seal storage layer 9 and can seal the carbon dioxide in the storage layer 9 from upward dissipation, has the characteristics of high clay content, good continuity, large thickness and the like, and the porosity of the cover layer 3 is generally less than 5 percent, and the permeability is less than 1mD.\|[0096] Then, perforating 4 is carried out on the inner wall of the corresponding cover layer 3 of the shaft 2, and the perforating 4 is communicated with the cracks 7 of the drilling annular cement 5 and the surrounding rock breaking belt 6;\|[0097] when drilling is excavated, after the shaft 2 passes through the cover layer 3, the cover layer around the shaft 2 is damaged, annular cement 5 and surrounding rock breaking zones 6 are formed around the shaft 2, and cracks 7 are large, so that carbon dioxide in a reservoir layer leaks out through the cracks 7. The plugging method of the invention is to plug the leakage.\|[0098] A relatively closed space is required in the wellbore 2 at the perforation interval at the corresponding cap prior to perforation to avoid the risk of significant amounts of carbon dioxide and water entering the wellbore 2 during perforation. The measures for setting the closed space are as follows: installing an upper packer 8 and a lower packer 8 on the inner wall of the well shaft corresponding to the cover layer 3 in the well shaft 2, wherein the two packers 8 isolate carbon dioxide sealed in a reservoir 9 below the cover layer 3 from water in an overburden stratum 10 above the cover layer; an injection pipe, also called a central pipe 18, is arranged on the upper packer 8, the upper pipe orifice of the central pipe 18 is connected with a lime milk suspension injection device fracturing truck 12 arranged on the wellhead, the fracturing truck 12 is connected with a stirring box, and lime milk suspension with required concentration is provided, so that the lime milk suspension is input into the closed space through the injection pipe at a certain speed, and then is injected into the perforation.\|[0099] Preferably, the distance of the packer from the perforation section during the step of setting the packer is greater than 2.5m. The distance of the packer in the upper part from the upper edge of the cover layer is > 2.5 meters. The distance of the packer in the lower part from the lower edge of the cover layer is > 2.5 meters. The aperture of the perforations 4 is controlled to be 5-20mm, in this embodiment, for example, 7mm. The density of perforations is 10 holes/meter-30 holes/meter, in this embodiment, 20 holes/meter in the perforation section. The ratio of the height of the perforating section to the height of the cover layer is 0.1-0.9, the ratio value is selected in relation to the thickness of the cover layer, the thickness of the cover layer is generally tens of meters to hundreds of meters, when the thickness of the cover layer is thinner, the ratio value is slightly larger, and when the thickness of the cover layer is thicker, the ratio value is slightly smaller, so that the height of the perforating section is ensured to be more suitable for 5-30 meters. Preferably, the spacing between the upper and lower edges of the perforation section and the upper and lower edges of the cap layer is greater than 5 meters. In this embodiment, both pitches are, for example, 8 meters.\|[0100] According to the invention, lime milk is injected into the perforation of the cover layer, and on annular cement and surrounding rock fracture zones where cracks appear due to the damage of drilling on the cover layer, the lime milk and carbon dioxide meet and react in the cracks to generate calcium carbonate to fill and seal the cracks, so that the cover layer is repaired. Therefore, the aperture and density of the perforation can influence the state that the lime milk suspension enters the cracks, if the aperture of the perforation is too small, the flow of the lime milk can be blocked, so that the contact between the lime milk and the carbon dioxide is poor, but if the aperture is too large, the cover layer can be damaged greatly, the repairing difficulty is increased, and the distribution of the lime milk in the drilling annulus cement 5 and the surrounding rock breaking zone 6 can be influenced by the density of the perforation. The proper aperture and density of the perforation are selected, and the position and the height of the perforation section in the cover layer can influence the stability and the firmness of cementing the surrounding rock breaking zone and the annular cement of the fractured well into a compact whole and the high efficiency of plugging construction.\|[0101] It is also a good measure that the perforation segments are evenly distributed over the entire circumference of the inner wall of the well. Because the crack position is not well controlled, the position where the crack possibly appears can be fully covered by the uniform perforation, and a better plugging effect can be obtained.\|[0102] The next step is to perform the plugging by injecting a lime milk suspension into the enclosed space, i.e. into the perforations 4. Preparing lime milk suspension (Ca (HO) with initial set concentration not less than 2mol/L (2-10 mol/L) by using a stirring box 11 arranged on a wellhead 2 Colloidal solution), for example, an initial set concentration of 5mol/L, is slowly injected into the perforation section by means of the fracturing unit 12 through the central conduit 18 at a rate of less than 0.5L/s, for example, 0.3L/s, when the injection pressure P is higher than the reservoir pressure P 0 A threshold value, for example, 0.5MPa, which is a value of 0.2 times the initial injection concentration, i.e., the concentration is reduced to 1mol/L, and then the injection is continued slowly at a rate of 0.3L/s, and when the injection pressure P is raised again by a threshold value of 0.5MPa, the concentration of the lime milk suspension is reduced again to 0.2 times the previous concentration, i.e., the concentration is reduced to 0.2mol/L, and the injection is continued, and the cycle is continued until the lime milk concentration is equal to or less than the formation temperature, i.e., the temperature of the carbon dioxide reservoir 9, ca (HO 2 For example, the temperature of reservoir 9 is 60 ℃, ca (HO) at this time 2 The solubility of (C) was 0.02mol/L. Thus, when the injection pressure is increased by two more thresholds, the concentration of milk of lime is reduced to Ca (HO) at the formation temperature 2 Is a solvent for the polymer. At this time, the injection was continued at a concentration of 0.02mol/L, the concentration of lime milk was not lowered any more, and the above-mentioned solubility was the final set concentration. Continuing the injection at this final set concentration, the injection pressure gradually increases and, when increasing to an injection termination set pressure, the injection ends. This injection termination set pressure was 1.0MPa.\|[0103] As another example, where the initial set concentration of milk of lime is 10mol/L, the threshold value is also 0.5MPa when the injection pressure P reaches a value higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 2mol/L, the injection is continued, and when the injection pressure P is higher than the reservoir pressure P again 0 At 0.5MPa, the concentration is reduced to 0.4 mol/L again, the injection is continued, and the third injection pressure is higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 0.08 mol/L, and the fourth injection pressure is higher than the reservoir pressure P 0 At 0.5MPa, the concentration is reduced to 0.016 mol/L, which is lower than the solution degree of 0.02mol/L, and at this time, the solution is injected at the final set concentration, namely the solubility, until the injection pressure is 1.0MPa.\|[0104] The pressure difference of the threshold value and the thickness of the cement sheath can calculate the stratum permeability, and when the parameters are set, the calculated stratum permeability of the cement sheath is close to the stratum permeability of the cover layer, and the closed crack under the lime milk concentration condition can be considered to be not leaked. The fact that a threshold value is reached indicates that the lime milk with the existing concentration is not easy to continue to be injected, so that the concentration needs to be reduced, the concentration is reduced by a constant multiple, the operation is facilitated, and more importantly, the completion of plugging of fine cracks can be achieved gradually.\|[0105] In the injection process, the concentration of lime milk is adjusted, and initially, the concentration is larger, larger cracks are filled as soon as possible, then the concentration is reduced, lime milk with lower concentration easily enters smaller cracks, and fine cracks can be plugged. At the initial set concentration, the plugging can be completed within 10 times of concentration reduction according to the rate reduction of 0.2 times, and the setting is ideal. If the initial set concentration is too low, an integral structure with good plugging performance is not easy to form. However, if the initial set concentration is too high, the lime milk is too thick, and besides the problems of the above and the increase of the concentration reduction times, ports of some cracks are sealed by the thick lime milk, so that the whole annular cement and the size cracks in the surrounding rock breaking zone are not filled, and the sealing effect is also affected.\|[0106] The lowest final set concentration of milk of lime is not lower than the solubility at the temperature of the reservoir 9, which serves to let the milk of lime suspension sufficiently enter the fissures 7 at a set final set pressure (e.g. 1.0 MPa). But the final set concentration must not be below the solution level, otherwise, the subsequent injection of unsaturated lime water will have a damaging effect on the calcium carbonate formed by the reaction of the previously injected lime milk with carbon dioxide.\|[0107] The injection rate described above also affects the occlusion effect. The invention provides a maximum rate limit of 0.5 liter/second at which lime milk entering the crack can react with leaked carbon dioxide in good time to form calcium carbonate to seal the crack. If the speed limit is too high, the blocking effect is not good, but if the speed limit is too low, the blocking is not easy to proceed and the blocking efficiency is too low.\|[0108] The plugging effect monitoring step follows.\|[0109] Monitoring can also be performed by using a gas flow meter provided at the wellhead to measure the gas flow at the wellhead. A wellhead vent valve, which is a valve to a gas flow meter, may also be closed, and the wellhead perimeter carbon dioxide concentration monitored to determine the leak path of carbon dioxide along the abandoned borehole.\|[0110] Alternatively, a monitoring well 13 may be drilled on the side of the well, the well depth of which does not exceed the cap layer 3.\|[0111] Ph value probes (14), an earth surface carbon dioxide concentration meter (15) and a wellhead gas flowmeter (16) are placed in a monitoring well (13) to be matched for use, the Ph value of overlying stratum water, the wellhead periphery carbon dioxide concentration and wellhead carbon dioxide leakage are continuously monitored, and data are analyzed through an earth surface monitoring station (17).\|[0112] The frequency of monitoring may be generally such that data is taken every 12 hours.\|[0113] If no carbon dioxide leakage is found in the 30-day monitoring, the plugging is considered to be successful, and then the following process steps are carried out: and (5) sealing the well.\|[0114] The bridge plug well sealing in the well can be implemented, and the sealing of the leakage of the carbon dioxide along the abandoned well is completed.\|[0115] Firstly, taking out the packer at the upper part of the perforation section, injecting carbon dioxide corrosion resistant cement and the like into the perforation section in the well to form a cement bridge plug for preventing leakage in the well, and integrally completing the plugging of the leakage of carbon dioxide along the abandoned well. The carbon dioxide corrosion resistant cement can be slag cement, volcanic ash cement, fly ash cement or composite cement, etc., and the concrete method of well sealing belongs to the prior art and is not repeated here.\|[0116] If the sealing is not up to standard through monitoring, the leakage reason needs to be specifically analyzed, if the leakage is still caused by the crack around the drilling well, the perforation 4 can be set at a new position again, lime milk can be refilled, at this time, the concentration of the lime milk can be adjusted, for example, the set concentration is increased, and the lime milk can be refilled. And then monitoring the blocking effect until the blocking reaches the standard.\|[0117] According to the invention, the cover layer is preferably perforated, a shaft with leakage risk, drilling annulus cement and a surrounding rock breaking belt are communicated, a packer is arranged in the shaft, a relatively closed space is formed in a perforation section, lime milk suspension is slowly injected into the perforation section through a fracturing truck, the injection pressure is controlled in the process, the concentration of lime milk is gradually reduced, lime milk in a crack reacts with leaked carbon dioxide to form hardened and compact calcium carbonate, and a carbon dioxide leakage channel is further plugged. The invention can effectively block the crack channel leaked along the abandoned well in the geological carbon dioxide sealing process, and can bond the surrounding rock breaking zone and the crack-containing drilling annular cement into a compact whole, thereby greatly reducing the risk of leakage along the abandoned well in the geological carbon dioxide sealing process. The injected lime milk suspension reacts with the carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, so that the risk of geological environment pollution is extremely low, and the plugging process is safe and environment-friendly.	Family Number\|(96423759)\|96423759\|Object of Invention\|(CN113494265 A)\|( . . . ) well in a carbon dioxide geological storage process , which comprises the steps of perforating a stable cover layer on a carbon dioxide geological storage layer , communicating a shaft with leakage risk , drilling annular cement and a surrounding rock crushing zone , injecting lime milk suspension into a perforating section , enabling the lime milk in a gap to react with leaked carbon dioxide to form hardened compact calcium carbonate , and further blocking a carbon dioxide leakage channel . \|Advantages / Prev. Drawbacks\|(CN113494265B B)\|At present , great project demonstration of carbon capture utilization and sealing is developed in each industry of China , and a foundation is laid for subsequent large - scale carbon dioxide injection . \|(CN113494265 A)\|At present , the research on the sealing technology of leakage along a drilling well in the geological carbon dioxide sequestration process is very limited , and the current situation is not favorable for solving the problem of sudden leakage along a waste drilling well in the geological carbon dioxide sequestration process , so that the development of a great environmental protection project of underground carbon dioxide sequestration is limited to a great extent . \|Independent Claims\|(CN113494265 A)\|1. A method for plugging leakage along abandoned wells in the geological carbon dioxide sequestration process is characterized by comprising the following steps : the method comprises the following steps : ( . . . ) \|	Civil engineering	E21B-033/13\|E21B-033/138		E21B-033/13\|E21B-033/138	E21B-033/13\|E21B-033/138	E21B-033/13\|E21B-033/138			CN119715293\|CN117365368\|CN116906838\|CN117703328\|CN115387755\|CN114086915\|US12560053\|CN117347111B\|CN116771414B\|CN115405255B\|CN114163982B	CN119715293 113979591 WHO=Examiner SELF=N CAT=A\|CN117365368 108075309 WHO=Examiner SELF=N CAT=A\|CN116906838 106902088 WHO=Examiner SELF=N CAT=A\|CN117703328 108903396 WHO=Examiner SELF=N CAT=A\|CN115387755 102721841 WHO=Examiner SELF=N CAT=A\|CN114086915 98867716 WHO=Examiner SELF=N CAT=A\|US12560053 115114287 WHO=Applicant SELF=N\|CN117347111B 108069478 WHO=Examiner SELF=N\|CN116771414B 106534659 WHO=Examiner SELF=N\|CN115405255B 102795999 WHO=Examiner SELF=N\|CN114163982B 99082908 WHO=Examiner SELF=N	CN111622746\|CN110284853\|CN105156066\|CN109577908\|CN106382109\|CN108026766\|CN102144074\|WO200662433\|US5035813	CN111622746 90481716 WHO=Examiner SELF=N CAT=Y\|CN110284853 86162646 WHO=Examiner SELF=N CAT=Y\|CN105156066 71726885 WHO=Examiner SELF=N CAT=Y\|CN109577908 84048491 WHO=Examiner SELF=N CAT=A\|CN106382109 75321301 WHO=Examiner SELF=N CAT=A\|CN108026766 74494517 WHO=Examiner SELF=N CAT=A\|CN102144074 1845506 WHO=Examiner SELF=N CAT=A\|WO200662433 36247452 WHO=Examiner SELF=N CAT=A\|US5035813 35696446 WHO=Examiner SELF=N		WO200662433; CN102144074; CN105156066; CN106382109; CN108026766; CN109577908; CN110284853; CN111622746; US5035813		LAPSED	(CN113494265)\|LAPSED	DEAD	(CN113494265)\|DEAD	(CN113494265)\|LEGAL DETAILS FOR CN113494265\|Actual or expected expiration date=2025-07-18\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2021-07-23\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202110837467\|Application date=2021-07-23\|Standardized application number=2021CN-0837467\|Event publication date=2021-10-12\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN113494265\|Publication stage code=A\|Publication date=2021-10-12\|Standardized publication number=CN113494265\|Event publication date=2021-10-12\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2021-10-29\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2023-05-02\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN113494265\|Publication stage code=B\|Publication date=2023-05-02\|Standardized publication number=CN113494265B\|Event publication date=2023-05-02\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2025-07-18\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee			https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTId3YEhR1wxhj8BQAJLzMlbZEW38EL5eDPpKOoVIJxKQ7GsFqRuZutXlT5jEXwVJs=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000067606327&ekey=2079&xpn=CN113494265B&kind=B	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=TDcyjbThyfq0YYqkBFXZbbmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN113494265)\|CN\|(CN113494265)\|CN	(CN113494265)\|NAME=CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS , COUNTRY=CN\|(CN113494265)\|NAME=CENTER FOR HYDROGEOLOGY & ENVIRONMENTAL GEOLOGY CGS , COUNTRY=CN		(CN113494265)\|NAME=CHEN YING;BEIJING BEIXIN-ZHICHENG INTELLECTUAL PROPERTY AGENT CO., LTD. , REG=11100\|(CN113494265)\|NAME=CHEN YING;BEIJING BEIXIN-ZHICHENG INTELLECTUAL PROPERTY AGENT CO., LTD. , REG=11100		(CN113494265)\|NAME=FU LEI\|NAME=MA XIN\|NAME=DIAO YUJIE\|NAME=ZHANG CHENGLONG\|NAME=LIU TING\|NAME=Fu Jie\|NAME=SHAO WEI\|(CN113494265)\|NAME=FU LEI\|NAME=MA XIN\|NAME=DIAO YUJIE\|NAME=ZHANG CHENGLONG\|NAME=LIU TING\|NAME=Fu Jie\|NAME=SHAO WEI	(CN113494265)\|2	1	1					(CN113494265)\|Number of Claims: NCL=9\|Gazette date: GAZDATE=2023-05-02\|Gazette number: GAZNUM=39-1801\|Number of Pages: NPAGES=13\|Primary examiner: 柳思源\|Primary examiner: Liu Siyuan\|\|(CN113494265)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2021-10-12\|Gazette number: GAZNUM=37-4201\|Number of Pages: NPAGES=13\|Primary examiner: 柳思源\|Primary examiner: Liu Siyuan\|	(CN113494265)\|Previous publication: CN113494265 A 2021-10-12 [CN113494265]	(CN113494265)\|CHINESE (CHI)	(CN113494265B)\|Patent\|(CN113494265)\|Patent	Titre: (CN113494265)\|Plugging method for leakage along abandoned well in carbon dioxide geological storage process Résumé: (CN113494265)\|The invention provides a method for blocking leakage along an abandoned well in the geological storage process of carbon dioxide. The method comprises the following steps that perforating is carried out by adopting a stable cover layer above a geological storage layer of carbon dioxide; a shaft with leakage risk, drilling annular cement and a surrounding rock fracture zone communicate with one another; and lime milk turbid liquid is injected into a perforation interval, so that lime milk in a gap reacts with leaked carbon dioxide to form hardened and compact calcium carbonate, and a carbon dioxide leakage channel is blocked. According to the method for blocking leakage along the abandoned well in the geological storage process of carbon dioxide, the crack channel leaking along the abandoned well in the geological storage process of carbon dioxide can be effectively blocked, meanwhile, a surrounding rock broken zone and crack-containing drilling well annulus cement can be cemented into a compact whole, and the risk of leaking along the abandoned well in the geological storage process of carbon dioxide is greatly reduced. The injected lime milk turbid liquid reacts with carbon dioxide leaked along the abandoned well to generate common calcium carbonate and water in the stratum, the geological environment pollution risk is extremely low, and the plugging process is safe and environmentally friendly.	36	Abstract	gpt-4o-mini	no	The article focuses on a method for blocking CO₂ leakage in geological storage, not on accelerating mineral weathering or carbon sequestration through enhanced weathering processes.
37	CN202310241385	CN202310241385	CN116359471	105563865	CN116359471 A 2023-06-30 [CN116359471]	2023-03-09	2023-03-09	2023-06-30		(CN116359471)\|2043-03-09	(CN116359471)\|System and method for dynamically simulating mineralized sealed carbon dioxide filled goaf	(CN116359471)\|The invention discloses a system and method for dynamically simulating mineralized sealed carbon dioxide filled goaf, and belongs to the technical field of mineralized sealed carbon dioxide. The device is provided with a mineralization reaction device, a transportation device and a mineralization simulation device, the mineralization reaction device is composed of a reaction main body, an ultrasonic generation device and a bubble generation device, the transportation device is provided with a transportation pipeline and a pipeline monitoring device, and the mineralization simulation device comprises a triaxial loading device and a heating device. The triaxial loading equipment is provided with a material supporting part and a loading assembly. The mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline connector of the transportation device, so that the mineralization reaction system is formed, then the mineralization sealed carbon dioxide filling goaf is dynamically simulated through the mineralization reaction system, and the method is simple and convenient in simulation operation, economical and feasible and conforms to the concept of green mining.	ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY\|SHANDONG UNIVERSITY OF SCIENCE & TECHNOLOGY	(CN116359471)\|ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY ([CN])\|SHANDONG UNIVERSITY OF SCIENCE & TECHNOLOGY	WANG CHANGXIANG\|LU YAO\|ZHOU YONGQIANG\|LU WEI\|LI JINLIANG\|LI JINHU\|ZHUO HUI\|ZHANG QINGSONG\|ZHAO SHUJIE\|LI QINGHAI\|SI LEILEI\|JIANG NING	(CN116359471)\|WANG CHANGXIANG\|LU YAO\|ZHOU YONGQIANG\|LU WEI\|LI JINLIANG\|LI JINHU\|ZHUO HUI\|ZHANG QINGSONG\|ZHAO SHUJIE\|LI QINGHAI\|SI LEILEI\|JIANG NING	(CN116359471)\|LONG JUNBO;WEIHAI HENG YU RUN DA PATENT AGENCY OFFICE (GENERAL PARTNERSHIP)\|Reg. Nb: 37260	(CN116359471)\|Carbon dioxide emission and effective treatment are the key problems of attention in various fields, and the proposal of carbon dioxide mineralization sealing gives a solution thought, wherein the carbon dioxide mineralization sealing mainly imitates and accelerates the process of rock weathering and carbon dioxide absorption in nature, carbon dioxide is dissolved in water to generate carbonic acid, then the carbonic acid reacts with alkaline minerals to generate stable solid carbonate, and the stable solid carbonate can not be decomposed in long geological years, so that the permanent sealing of the carbon dioxide can be realized. Because the carbon emission proportion in the coal mine industry is higher, a certain carbon fixation measure is necessary for the coal mine industry, and the mining of coal resources can cause rock stratum movement and ground surface damage, so that goafs need to be filled; the large-scale experiment is limited in site, so that the mineralization filling process of the goaf is simulated in a laboratory in a simulation mode, the practical production significance is great according to the experimental result, the mode is convenient, the economy and the feasibility are realized, and the idea of green exploitation is met.\|	(CN116359471)\|1. A system for dynamically simulating mineralization and sequestration of carbon dioxide filling goaf, comprising: the mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment; the conveying device is provided with a conveying pipeline and a pipeline monitoring device; the mineralization simulation device comprises a triaxial loading device and a heating device, wherein the triaxial loading device is provided with a material supporting part and a loading assembly.\|	(CN116359471)\|The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|The invention discloses a system and a method for dynamically simulating mineralization and carbon dioxide sealing and filling goaf, which belong to the technical field of mineralization and carbon dioxide sealing; the device comprises a mineralization reaction device, a transportation device and a mineralization simulation device, wherein the mineralization reaction device consists of a reaction main body, ultrasonic generating equipment and bubble generating equipment, the transportation device is provided with a transportation pipeline and a pipeline monitoring device, the mineralization simulation device comprises a triaxial loading equipment and a heating equipment, and the triaxial loading equipment is provided with a material supporting part and a loading assembly.\|The invention provides a system for dynamically simulating mineralization to seal carbon dioxide to fill a goaf, aiming at the technical problems in the prior art.\|	(CN116359471)\|CARBON DIOXIDE(100,81)\|SIMULATING MINERALIZATION(100,12)\|FILLING GOAF(100,3)\|CARBON DIOXIDE FILLING GOAF(100,1)\|SEQUESTRATION(100,1)\|MINERALIZATION SIMULATION(66,32)\|MINERALIZATION REACTION(44,49)\|COAL RESOURCE MINING(41,1)\|GREEN EXPLOITATION IDEA(37,1)\|MINERALIZATION SIMULATION AIRTIGHTNESS(33,3)\|COAL MINE INDUSTRY(29,2)\|TRIAXIAL LOADING(28,28)\|GOAF(27,22)\|TRIAXIAL LOADING EQUIPMENT(26,4)\|CONVEYING PIPELINE(25,6)\|MINERALIZATION SEALING(25,1)\|MINERALIZE SIMULATION(25,1)\|TRANSPORTATION PIPELINE(24,4)\|COAL RESOURCE(24,1)\|MINERALIZE PARTY(22,1)\|PASTE FILLING(21,31)\|GENERATING ULTRASOUND EQUIPMENT(20,3)\|CARBON DIOXIDE SEALING(20,2)\|ALKALINE MINERAL(20,1)\|MINERALIZATION(19,17)\|GREEN EXPLOITATION(18,3)\|STABLE SOLID CARBONATE(18,2)\|CARBON DIOXIDE MINERALIZATION SEALING(18,1)\|PRODUCTION SIGNIFICANCE(18,1)\|CARBON DIOXIDE SEQUESTRATION(17,2)\|LONG GEOLOGICAL YEAR(17,1)\|BUBBLE(16,20)\|HEATING EQUIPMENT(16,5)\|SIMULATION MODE(15,1)\|REACTION TANK(14,32)\|REACTION MAIN(14,7)\|FEASIBILITY(14,1)\|PASTE SLUMP(13,4)\|CARBON DIOXIDE MINERALIZATION(13,2)\|STABLE SOLID(13,2)\|CARBON EMISSION PROPORTION(13,1)\|ROCK STRATUM MOVEMENT(13,1)\|SOLUTION THOUGHT(13,1)\|ELECTROMAGNETIC FLOWMETER(12,10)\|CARBIDE SLAG(12,4)\|GOAF STRESS CONDITION(12,2)\|CARBON DIOXIDE ABSORPTION(12,1)\|CARBON DIOXIDE EMISSION(12,1)\|ECONOMY(12,1)\|LABORATORY(12,1)\|MEASURING CARBON FIXATION(12,1)\|LOADING BAFFLE(11,5)\|LOADING EQUIPMENT(11,4)\|CARBONIC ACID(11,2)\|GOAFS(11,1)\|SAMPLING PORT(10,2)\|CARBON DIOXIDE FILLED GOAF(10,1)\|CONVERSION EQUIPMENT(10,1)\|GAS OUTLET(9,10)\|CARBON DIOXIDE CONTENT(9,9)\|MINERALIZE REACTION MATERIAL(9,2)\|ROCK(9,1)\|CARBON DIOXIDE(8,2)\|DETECTION SENSOR(8,2)\|MONITORING EQUIPMENT(8,2)\|CARBON FIXATION(8,1)\|AQUEOUS SOLUTION(7,12)\|GAS SAMPLE(7,5)\|CARBON DIOXIDE BUBBLE(7,3)\|CONVEYING CONDITION(7,3)\|GOAF AREA(7,2)\|MINERALIZATION SIMULATOR(7,2)\|TRANSPORTATION DEVICE(6,16)\|ULTRASOUND(6,11)\|MICRO BUBBLE GENERATOR(6,8)\|ULTRASONIC GENERATING(6,7)\|GANGUE(6,4)\|MONITORING DATA(6,2)\|TRIAXIAL LOADING EXPERIMENT(6,2)\|FILLING PUMP(5,6)\|FLY ASH(5,4)\|GOAF MINERALIZATION AREA(5,4)\|DATA COLLECTION(5,3)\|LAYERING CHANGE VALUE(5,2)\|GROUND SURFACE DAMAGE(5,1)\|LARGE SCALE EXPERIMENT(5,1)\|MINERALIZATION REACTION TEST BLOCK(4,6)\|AIRTIGHTNESS(4,4)\|CARBON DIOXIDE GAS CYLINDER(4,4)\|ENVIRONMENT TEMPERATURE(4,4)\|NACL(4,4)\|TEMPERATURE COLLECTING DATA(4,3)\|COAGULATED TEST INTERNAL BUBBLE(4,2)\|EXPERIMENTAL TOOL(4,2)\|PASTE LAYERING CHANGE(4,2)\|REACTION SOLIDIFICATION(4,2)\|SILICA FUME(4,2)\|SIMULATED FLUE GAS PROPORTIONING(4,2)\|TRIAXIAL LOADING SLOT(4,2)\|ULTRASONIC WAVE CAVITATION(4,2)\|AFTER TRIAXIAL LOADING TEST(4,1)\|CONTENT NUMERIC VALUE CHANGE(4,1)\|ELECTROMETHOD INSTRUMENT(4,1)\|GOAF MINERALIZATION REGION(4,1)\|MINERALIZATION LOADING EXPERIMENT(4,1)\|TRIAXIAL LOADING GROOVING HEAD(4,1)\|TRIAXIAL LOADING NOTCH(4,1)\|SEALING(3,14)\|INTELLIGENT CONTROL(3,11)\|MATERIAL SAMPLING(3,9)\|PIEZORESISTIVE PRESSURE SENSOR(3,8)\|SENSOR INTERFACE(3,5)\|ULTRASONIC TRANSDUCER(3,4)\|BUBBLE GENERATION EQUIPMENT(3,2)\|CETYLTRIMETHYLAMMONIUM BROMIDE(3,2)\|COAGULATION TEST(3,2)\|DATA ACQUISITION(3,2)\|FILLING SITE(3,2)\|GAS TIGHTNESS(3,2)\|NEGLIGIBLE CONTENT(3,2)\|POSITIONAL RELATIONSHIP(3,2)\|SIMULATION EXPERIMENT(3,1)\|GAS COMPONENT ANALYSIS(2,5)\|LOAD PRESSURE HEAD(2,4)\|LOADING PLATE(2,4)\|PLACING MATERIAL AREA(2,4)\|WATER GLASS(2,4)\|MATERIAL TRANSPORTATION PIPELINE(2,3)\|PIPELINE TRANSPORTATION(2,3)\|CTABS(2,2)\|ELECTRICAL TOOL(2,2)\|FILLING VOLUME(2,2)\|FLOWMETER(2,2)\|GAS REACTION(2,2)\|BUBBLE STABILITY(2,1)\|CARBON DIOXIDE MICROBUBBLE(2,1)\|FOAM STABILIZER(2,1)\|GROOVE DIMENSION(2,1)\|IMMOBILIZED(2,1)\|INTENSIFICATION(2,1)\|LOADING GROOVING PRESS HEAD(2,1)\|LOADING STRESS(2,1)\|MICRO NANO BUBBLE MODE(2,1)\|MINERALIZATION REACTION TEST PROPORTION(2,1)\|MINERALIZE REACTION TESTTHE BLOCK(2,1)\|SYMBOL MARK(2,1)\|	(CN116359471)\|1. A system for dynamically simulating mineralization and sequestration of carbon dioxide filling goaf, comprising:\|the mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment;\|the conveying device is provided with a conveying pipeline and a pipeline monitoring device;\|the mineralization simulation device comprises a triaxial loading device and a heating device, wherein the triaxial loading device is provided with a material supporting part and a loading assembly.\|2. The system for dynamically simulating mineralization and sealing of carbon dioxide filling goaf according to claim 1, wherein the reaction main body is provided with a reaction tank, a stirring device is arranged in the reaction tank, the ultrasonic generating equipment is connected with the reaction tank through a conversion equipment, and a carbon dioxide gas cylinder is connected to the bubble generating equipment.\|3. The system for dynamically simulating mineralization, sealing and carbon dioxide filling of goaf according to claim 1, wherein the mineralization simulation device comprises a maintenance part, a loading part and a forming part, the loading part is provided with a material placing area, the peripheral side of the material placing area is provided with a loading pressure head and a loading baffle, and the heating equipment arranged on the forming part is arranged on the lower side of the loading part.\|4. A method for dynamically simulating mineralization and sequestration of carbon dioxide to fill goaf, characterized in that it uses the system for dynamically simulating mineralization and sequestration of carbon dioxide to fill goaf according to any one of claims 1-3, said method comprising the following steps:\|weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|adding water into the bubble generating equipment, then introducing carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into the mineralization reaction device for mineralization reaction;\|conveying the fully mixed mineralized filling paste through the conveying device, collecting data of temperature and pressure in the system, sampling and analyzing the filling paste at an output port through a sampling port, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through the pipeline monitoring device;\|the conveyed mineralized filling paste is conveyed into the mineralization simulation device through a conveying pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and then the mineralized material is naturally cured until the mineralized material is completely solidified;\|at the moment, a triaxial loading test is carried out, a stress condition of the goaf is simulated through triaxial loading equipment, a test block is loaded, and the temperature of a mineralized area of the goaf is simulated through changing the forming environment temperature of the test block through heating equipment;\|after the loading test is finished, extracting gas through the gas outlet hole, carrying out secondary gas component analysis, and comparing an analysis result with a primary component analysis result;\|and finally, completely extracting the gas in the mineralization simulation device through the gas outlet hole, analyzing the gas components to obtain the content change of carbon dioxide in the gas, and judging the mineralization effect of the mineralized material according to the carbon dioxide content numerical value change.\|5. The method for dynamically simulating mineralizing and sequestering carbon dioxide to fill a goaf according to claim 4, wherein the mineralizing reaction material comprises water glass, fly ash, carbide slag, gangue, naOH, naCl, CTAB, H 2 O 2 。\|6. The method for dynamically simulating mineralizing and sequestering carbon dioxide to fill the goaf according to claim 5, wherein the mineralizing reaction material comprises the following components in percentage by mass: 3:7:3:3.\|7. the method for dynamically simulating mineralized and sealed carbon dioxide filling goaf according to claim 4, wherein the mineralized reaction device is connected with the mineralized simulation device through the transportation device to form a test system, and the test system is further provided with an intelligent control system for intelligent control and data monitoring.\|8. The method for dynamically simulating mineralized and sealed carbon dioxide filled goaf according to claim 4, wherein when the mineralized and filled paste is conveyed by the conveying device, data acquisition is carried out on monitoring equipment in the pipeline monitoring device and the mineralization reaction device once every 1 minute, sampling analysis is carried out on the filled paste at an output port of the conveying device every 5 minutes, and analysis on paste slump and paste layering change values is carried out on samples.\|9. The method for dynamically simulating mineralizing, sequestering and carbon dioxide filling a goaf according to claim 4, wherein the temperature and pressure in the system are monitored by the detection sensor when the mineralizing simulation device is heated by the heating equipment in a triaxial loading test, and the mineralizing party is considered to be finished when the pressure in the device is kept unchanged for a long time.\|10. The method for dynamically simulating mineralized and sealed carbon dioxide filling goaf according to claim 4, wherein the content of carbon dioxide fixed by bubbles in the test block after triaxial loading test can be obtained according to the known total amount of the carbon dioxide gas cylinder, the content of carbon dioxide introduced into the system and the content of carbon dioxide theoretically absorbed by the mineralized reaction material, and the mineralized effect of the mineralized material can be judged by the value.	(CN116359471)\|TECHNICAL FIELD\|[0001] The invention belongs to the technical field of mineralized and sealed carbon dioxide, and particularly relates to a system and a method for dynamically simulating mineralized and sealed carbon dioxide to fill a goaf.\|BACKGROUND ART\|[0002] Carbon dioxide emission and effective treatment are the key problems of attention in various fields, and the proposal of carbon dioxide mineralization sealing gives a solution thought, wherein the carbon dioxide mineralization sealing mainly imitates and accelerates the process of rock weathering and carbon dioxide absorption in nature, carbon dioxide is dissolved in water to generate carbonic acid, then the carbonic acid reacts with alkaline minerals to generate stable solid carbonate, and the stable solid carbonate can not be decomposed in long geological years, so that the permanent sealing of the carbon dioxide can be realized.\|[0003] Because the carbon emission proportion in the coal mine industry is higher, a certain carbon fixation measure is necessary for the coal mine industry, and the mining of coal resources can cause rock stratum movement and ground surface damage, so that goafs need to be filled; the large-scale experiment is limited in site, so that the mineralization filling process of the goaf is simulated in a laboratory in a simulation mode, the practical production significance is great according to the experimental result, the mode is convenient, the economy and the feasibility are realized, and the idea of green exploitation is met.\|DISCLOSURE\|Disclosure of Invention\|[0004] The invention provides a system for dynamically simulating mineralization to seal carbon dioxide to fill a goaf, aiming at the technical problems in the prior art.\|[0005] In order to solve the technical problems, the invention comprises:\|[0006] the mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment;\|[0007] the conveying device is provided with a conveying pipeline and a pipeline monitoring device;\|[0008] and the mineralization simulation device comprises a triaxial loading device and a heating device, wherein the triaxial loading device is provided with a material supporting part and a loading assembly.\|[0009] Preferably, the reaction main body is provided with a reaction tank, a stirring device is arranged in the reaction tank, the ultrasonic generating equipment is connected with the reaction tank through a conversion device, and the bubble generating equipment is connected with a carbon dioxide gas cylinder.\|[0010] Preferably, the mineralization simulation device comprises a curing part, a loading part and a forming part, wherein the loading part is provided with a material placing area, the periphery side of the material placing area is provided with a loading pressure head and a loading baffle, and the heating equipment arranged on the forming part is arranged at the lower side of the loading part.\|[0011] The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|[0012] weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|[0013] adding water into bubble generating equipment, then introducing carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into a mineralization reaction device for mineralization reaction;\|[0014] conveying the fully mixed mineralized filling paste through a conveying device, collecting data of temperature and pressure in a system, sampling and analyzing the filling paste at an output port through a sampling port, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through a pipeline monitoring device;\|[0015] the conveyed mineralized filling paste is conveyed into a mineralization simulation device through a conveying pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and then the mineralized material is naturally cured until the mineralized material is completely solidified;\|[0016] at the moment, a triaxial loading test is carried out, a stress condition of the goaf is simulated through triaxial loading equipment, a forming environment temperature of the test block is changed through heating equipment, and the temperature of a mineralized area of the goaf is simulated;\|[0017] after the loading test is finished, extracting gas through the gas outlet hole, carrying out secondary gas component analysis, and comparing an analysis result with a primary component analysis result;\|[0018] and finally, completely extracting the gas in the mineralization simulation device through the gas outlet, analyzing the gas components to obtain the content change of carbon dioxide in the gas, and judging the mineralization effect of the mineralized material according to the numerical value change of the carbon dioxide content.\|[0019] Preferably, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 。\|[0020] Preferably, the mineralization reaction material comprises the following components in percentage by mass: 3:7:3:3.\|[0021] preferably, the mineralization reaction device is connected with the mineralization simulation device through the transportation device to form a test system, and the test system is also provided with an intelligent control system for intelligent control and data monitoring.\|[0022] Preferably, when the mineralized filling paste is conveyed by the conveying device, data acquisition is carried out on the pipeline monitoring device and monitoring equipment in the mineralization reaction device every 1 minute, sampling analysis is carried out on the filling paste at the output port of the conveying device every 5 minutes, and analysis on paste slump and paste layering change values is carried out on samples.\|[0023] Preferably, when a triaxial loading test is performed, the mineralization simulation device is heated by the heating equipment, the temperature and the pressure in the system are monitored by the detection sensor, and the mineralization is considered to be finished when the pressure in the device is kept unchanged for a long time.\|[0024] Preferably, the content of carbon dioxide fixed by bubbles in the test block after the triaxial loading test can be obtained according to the known total amount in the carbon dioxide cylinder, the content of carbon dioxide introduced into the system and the content of carbon dioxide theoretically absorbed by the mineralization reaction material, and the mineralization effect of the mineralization material can be judged according to the value.\|[0025] Compared with the prior art, the invention has the following beneficial effects:\|[0026] the invention has simple and convenient simulation operation, is economical and feasible, and accords with the concept of green exploitation; by adding foaming agents such as hydrogen peroxide, aluminum powder, silica fume and the like into the mineralized reaction material, the void ratio of the mineralized material after complete reaction solidification is improved, and the filling volume is enlarged; the method comprises the steps of generating an aqueous solution containing micro-nano carbon dioxide bubbles by a micro-nano bubble generating device from carbon dioxide gas and water, introducing a mineralization reaction material to promote mineralization reaction, improving mineralization reaction rate, combining mechanical stirring and ultrasonic waves, and promoting mineralization reaction by using cavitation of ultrasonic waves and mechanical stirring.\|[0027] The transportation device adopts a sectional type transportation pipeline to simulate the transportation of mineralized filling paste on a filling site, the mineralization simulation device simulates the stress condition of a goaf to load a mineralization reaction test block, the heating device changes the temperature of the test block to simulate the temperature of a mineralization area of the goaf, and the triaxial loading device performs triaxial loading experiments on the test block in the mineralization simulation device according to the stress condition of the filling goaf, so that the test environment is ensured to be more attached to a real operation environment, and the simulation result is feasible and effective; by analyzing the gas after loading, the aim of detecting whether the mineralized filling paste can realize goaf filling is fulfilled.\|DRAWINGS DESCRIPTION\|[0028] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are required for the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0029] FIG. 1 is a schematic structural view of a mineralization reaction device according to the present invention;\|[0030] FIG. 2 is a schematic view of a transportation device according to the present invention;\|[0031] FIG. 3 is a schematic top view of the mineralization simulator of the present invention;\|[0032] FIG. 4 is a schematic diagram of the front view of the mineralization simulator of the present invention.\|[0033] The symbol marks in the figures illustrate:\|[0034] 1. a reaction tank; 2. a mechanical stirring device; 3. a carbon dioxide microbubble generator; 4. a gas cylinder; 5. a gas control valve; 6. a flow meter; 7. an ultrasonic wave generating device; 8. an ultrasonic transducer; 9. a pressure sensor; 10. a temperature sensor; 11. a filling pump; 12. paste filling pipeline; 13. a delivery control valve; 14. mineralized material transport pipelines; 15. an electromagnetic flowmeter; 16. a piezoresistive pressure sensor; 17. a mineralized material sampling port; 18. a device body; 19. a material placement area; 20. a triaxial loading device; 21. loading an original pressure head by a triaxial; 22. triaxial loading grooving press heads; 23. loading a baffle; 24. an electric heating plate; 25. an electric hot plate controller; 26. sealing cover; 27. an air outlet hole; 28. a sensor interface; 29. an electrical method instrument.\|INVENTION MODE\|Detailed Description\|[0035] In order to make the technical problems, technical schemes and beneficial effects to be solved by the present application more clear, the present application is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the present application.\|[0036] Referring to fig. 1, the invention provides a system for dynamically simulating mineralization, sealing and carbon dioxide filling goaf, which comprises a mineralization reaction device, a transportation device and a mineralization simulation device, wherein the mineralization reaction device is connected with the mineralization simulation device through the transportation device to form a test system, and the test system is also provided with an intelligent control system, so that intelligent control and data monitoring of the system can be performed through the intelligent control system.\|[0037] The mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment.\|[0038] Specifically, the reaction main body is provided with a reaction tank 1 for mineralizing reaction materials; a mechanical stirring device 2 is arranged in the reaction tank 1, and the mineralization reaction can be promoted to be carried out through the mechanical stirring device 2; the upper end of the reaction tank 1 is connected with bubble generating equipment arranged at the outer end through a connecting pipeline, the bubble generating equipment comprises a carbon dioxide micro-bubble generator 3 and a gas cylinder 4, the gas cylinder 4 is connected to the carbon dioxide micro-bubble generator 3, and carbon dioxide is injected into the carbon dioxide micro-bubble generator 3 through the gas cylinder 4.\|[0039] Furthermore, the bubble generating equipment is also provided with a flowmeter 6 and a gas control valve 5, and the flowmeter 6 and the gas control valve 5 are arranged on a connecting pipeline connected with the outer end of the bubble generating equipment; the bubble generating device is used for improving the mineralization reaction efficiency by introducing carbon dioxide and water into the mineralization reaction device in a micro-nano bubble mode.\|[0040] As shown in fig. 1, the lower end of the reaction tank 1 is connected with an ultrasonic generating device through a connecting line, the ultrasonic generating device comprises an ultrasonic generating device 7 and an ultrasonic transducer 8, the ultrasonic transducer 8 is fixedly arranged at the bottom of the reaction tank 1, the ultrasonic generating device 7 is connected with the reaction tank 1 through the ultrasonic transducer 8, the power of ultrasonic waves can be controlled through the ultrasonic generating device 7, the mineralization effect can be improved, and the mineralization of carbon dioxide is promoted.\|[0041] Still further, the ultrasonic wave generating means 7 may be an ultrasonic wave generator or other ultrasonic wave generating device.\|[0042] Furthermore, a pressure sensor 9 and a temperature sensor 10 are also connected to the reaction tank 1 for monitoring the reaction pressure and the reaction temperature in the reaction tank 1.\|[0043] The reaction tank 1 is provided with a mineralization reaction material conveying port through which mineralization reaction materials can be added into the reaction tank 1; the bottom end of the reaction tank 1 is connected with a filling pump 11 and a paste filling pipeline 12, so that mineralized filling paste after being fully mixed is conveyed to a conveying device for conveying through the paste filling pipeline 12, and a conveying control valve 13 is arranged on the paste filling pipeline 12 and used for controlling the conveying of the mineralized filling paste.\|[0044] As shown in fig. 2, the transportation device comprises a plurality of sectional detachable connection type mineralized material transportation pipelines 14, an electromagnetic flowmeter 15 and a piezoresistive pressure sensor 16, wherein the electromagnetic flowmeter 15 is arranged at the inlet of the mineralized material transportation pipelines 14, and a mineralized material sampling port 17 is arranged at the outlet of the mineralized material transportation pipelines 14, so that sampling and monitoring are facilitated. The transportation device simulates the pipeline transportation of mineralized materials in a mineralized filling site, and the flow condition of the mineralized materials in the pipeline is monitored in real time through the electromagnetic flowmeter 15 and the piezoresistive pressure sensor 16.\|[0045] Further, a plurality of piezoresistive pressure sensors 16 are provided at a certain distance from each other inside the mineralized material transporting pipe 14 for pressure monitoring of the paste material transported in the pipe.\|[0046] As shown in fig. 3 and 4, the mineralization simulation device is an integrated treatment device for curing, molding and loading mineralization reaction materials, and comprises a curing part, a loading part and a molding part, wherein the curing part, the loading part and the molding part are all arranged in the device main body 18; the curing part is arranged in the loading part, and when the loading test is not performed, the curing part is used for performing natural curing of the mineralized material, and the loading part is used for performing a triaxial loading test of the mineralized material.\|[0047] Specifically, the curing part is a material placing area 19 arranged at the inner side of the loading part and used for placing mineralized materials for curing and loading test; the loading part is provided with a triaxial loading device 20, the compression strength of the sample after the mineralized material is loaded, analyzed and mineralized by the triaxial loading device 20, the triaxial loading device 20 comprises a triaxial loading original pressure head 21, a triaxial loading slotted pressure head 22, a loading baffle plate 23 and an electrical instrument 29, the triaxial loading slotted pressure head 22 is arranged at the inner end of the triaxial loading original pressure head 21 and is connected through threads, and the loading pressure head and the loading baffle plate 23 are arranged at the outer peripheral side of the material placing area 19.\|[0048] The shaping portion includes electric plate 24 and electric plate controller 25, and shaping portion sets up in the below of triaxial loading device 20, heats up mineralization analogue means through the electric plate 24 of shaping portion, detects temperature change through temperature sensor after the intensification, adjusts the scope of control mineralization analogue means inside temperature to the heating element, can also change the shaping ambient temperature of test block through electric plate 24 and simulate the temperature in goaf mineralization region moreover.\|[0049] Further, as a preferred embodiment of the present invention, the electric heating plate 24 is a constant temperature graphite electric heating plate.\|[0050] Further, as a preferred embodiment of the present invention, the loading plate 23 is disposed at the inner end of the triaxial loading slot die 22, the loading plate 23 has a square plate structure, and the triaxial loading slot die 22 can abut against the loading plate 23, so that a loading force can be applied to the sample placed in the material placement region 19; and the triaxial loading device 20 is provided with a plurality of groups of loading pressure heads and loading baffles 23 which are connected in a matched manner, so that triaxial loading tests can be carried out on the samples.\|[0051] Further, the loading baffle 23 is divided into an upper part and a lower part, the lower loading baffle is arranged on the base at the lower end, and the upper loading baffle and the lower loading baffle are connected with two ends of the notch of the triaxial loading slotting pressure head 22 through threads; the triaxial loading grooving head 22 is provided with a variety of grooving dimensions, the angle being variable, and the shape and size of the loading plate 23 being variable, so as to accommodate variations in the size and inclination of the mineralised reaction material.\|[0052] Specifically, as shown in fig. 4, the upper end of the device main body 18 is further provided with a sealing cover 26 for sealing the device, so as to ensure the air tightness of the device; the sealing cover 26 is provided with an air outlet 27 and a sensor interface 28, the air inside the device is sampled and detected through the air outlet 27, the bubble stability of the mineralized sample can be judged through detection, and the sensor interface 28 can be used for connecting a temperature sensor and a pressure sensor for temperature and pressure monitoring and controlling the loading process through an electromethod instrument 29.\|[0053] Furthermore, before closing the sealing cover 26, high vacuum silicone grease is applied to the contact surface between the sealing cover 26 and the loading part arranged at the lower side to ensure the air tightness of the device.\|[0054] Example 1\|[0055] The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|[0056] step 1: the mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline joint of the transportation device, so that a mineralization reaction system is formed.\|[0057] Step 2: the mineralized reaction material is weighed and prepared, and is filled into a mineralized reaction device.\|[0058] Specifically, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 The composition and the optimal proportion of each part of mineralization reaction material are shown in the following table.\|[0059] TABLE 1 mineralization reaction materials composition materials and proportion table thereof\|[0060] \|[0061] The CTABs listed in table 1 are cetyltrimethylammonium bromide.\|[0062] Specifically, the filling pump 11 and the delivery control valve 13 at the bottom end of the reaction tank 1 are closed, and the prepared mineralized reaction material is added into the reaction tank 1 through the mineralized reaction material delivery port.\|[0063] Step 3: opening a gas control valve 5 and a carbon dioxide micro-bubble generator 3 of the bubble generating equipment, firstly adding a certain amount of water into the carbon dioxide micro-bubble generator 3, then introducing carbon dioxide in a gas cylinder 4 into the carbon dioxide micro-bubble generator 3, generating an aqueous solution containing micro-nano carbon dioxide bubbles through the device, and then introducing the aqueous solution into a reaction tank 1 to start mineralization reaction; the mechanical stirring device 2 and the ultrasonic generating device 7 arranged in the reaction tank 1 are opened to improve the mineralization reaction efficiency of the reaction tank 1.\|[0064] After the mineralized reaction material and carbon dioxide in the reaction tank 1 fully react, a filling pump 11 and a conveying control valve 13 connected with the bottom end of the reaction tank 1 are opened, and the fully mixed mineralized reaction material is conveyed to a mineralization simulation device in a paste form through a paste filling pipeline 12 by a conveying device.\|[0065] Step 4: a piezoresistive pressure sensor 16, an electromagnetic flowmeter 15 and a mineralized material sampling port 17 in the transportation device are opened, and the transportation condition of mineralized filling paste in a transportation pipeline is observed; because the system is provided with the intelligent control system, the intelligent control system is utilized to collect data online, the pressure sensor, the temperature sensor and the electromagnetic flowmeter 15 in each experimental process collect data once every 60 seconds, and the filling paste at the output port of the conveying device is sampled and analyzed through the mineralized material sampling port every 5 minutes.\|[0066] Specifically, whether the filled paste can be transported smoothly in the pipeline without blocking the pipeline is judged by analyzing the data of the pressure sensor, the temperature sensor and the electromagnetic flowmeter, and whether the filled paste still can meet the paste pumping requirement after long-time pipeline transportation is judged by analyzing the paste slump and the paste layering change value of the sample of the mineralized material sampling port 17; the transportation condition of the filling paste in the pipeline is monitored in real time through the piezoresistive pressure sensor 16 and the sampling port to observe whether the mineralized filling paste can be transported smoothly.\|[0067] Step 5: opening a sealing cover 26 on the triaxial loading device 20, conveying the conveyed mineralized filling paste to a material placing area 19 in the mineralized simulation device through a conveying pipeline, and then closing the sealing cover 26 to ensure the air tightness in the device; the gas is sampled for the first time through the gas outlet 27 on the device main body 18, the sampled gas is subjected to component analysis through an experimental instrument, analysis data are recorded, and then the gas outlet 27 is closed to ensure the gas tightness of the device.\|[0068] The mineralized material is naturally cured for 12 hours, after 12 hours, the test block is completely solidified, and then a triaxial loading test can be carried out.\|[0069] Step 6: opening the sensor interface 28, and observing the change of the temperature and the pressure inside the device through the temperature and the pressure sensor; loading a mineralization reaction test block by simulating the stress condition of the goaf through a mineralization simulation device, and changing the temperature of the test block through an electric heating plate 24 of a forming part to simulate the temperature of a mineralization area of the goaf; the test block is subjected to a triaxial loading experiment according to the stress condition of the filled goaf by the triaxial loading device 20, and the forming environment temperature of the mineralized sample is changed by the electric heating plate 24.\|[0070] Step 7: when the sensor detects that the pressure in the device is kept unchanged for a long time, the mineralization reaction is finished, the air outlet 27 is opened to extract the air, the air in the device is collected for the second time, the analysis of the second air component is carried out, and the analysis result is compared with the analysis result of the first component;\|[0071] the existence condition of the internal bubbles of the coagulated test block after triaxial loading test with certain strength can be judged through comparison of the two groups of data, a part of bubbles are destroyed after triaxial loading, and the internal carbon dioxide gas is dispersed, so that the gas component of the loading device is changed, and the two gas analyses can be different.\|[0072] Step 8: finally, all the gases in the mineralization simulation device are extracted through the air outlet holes 27, and the gas component analysis is carried out to obtain the content change of carbon dioxide in the gases; according to the known total amount of the carbon dioxide gas cylinder, the content of carbon dioxide gas introduced into the system and the content of carbon dioxide which can be absorbed by the mineralization reaction material in theory, the content of carbon dioxide fixed by bubbles in the test block after the triaxial loading test can be obtained, and the mineralization effect of the mineralization material can be judged by the value.\|[0073] Therefore, the stability of the mineralized carbon dioxide can be verified, the efficiency of the mineralized reaction for absorbing the carbon dioxide can be calculated, and the compressive strength of the mineralized test block can be obtained through the damage condition of the test block after the triaxial loading test, so that whether the mineralized filling material can well fill the goaf can be judged.\|[0074] Example two\|[0075] The embodiment provides a method for dynamically simulating and mineralizing and sealing carbon dioxide in flue gas to fill a goaf, which comprises the following steps:\|[0076] step 1: the mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline joint of the transportation device, so that a mineralization reaction system is formed.\|[0077] Step 2: the mineralized reaction material is weighed and prepared, and is filled into a mineralized reaction device.\|[0078] Specifically, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 The composition and the optimal proportion of each part of mineralization reaction material are shown in the following table.\|[0079] TABLE 1 mineralization reaction materials composition materials and proportion table thereof\|[0080] \|[0081] The CTABs listed in table 1 are cetyltrimethylammonium bromide.\|[0082] Specifically, H 2 O 2 The CATB is a foam stabilizer.\|[0083] Specifically, the filling pump 11 and the delivery control valve 13 at the bottom end of the reaction tank 1 are closed, and the prepared mineralized reaction material is added into the reaction tank 1 through the mineralized reaction material delivery port.\|[0084] Step 3: using dried air and analytically pure CO 2 Proportioning of simulated flue gas, recording CO 2 The percentage of gas was set to a%.\|[0085] Since the composition of conventional fuel gas, fuel oil and coal flue gas is as follows: n (N) 2 :82%~89%,CO 2 :8%~15%,O 2 :3% -5%, a small amount of SO 2 Because of SO 2 The content of (C) is small, and the design is not considered, so that the dried air and pure CO for analysis are utilized 2 The composition of the flue gas can be simulated relatively accurately. (the normal air gas composition is as follows: N 2 :78%,O 2 21 percent of rare gas: 0.939%, CO 2 : 0.031), other gases and impurities: 0.03%).\|[0086] Step 4: opening a gas control valve 5 of a bubble generating device and a carbon dioxide micro-bubble generator 3, firstly adding a certain amount of water into the carbon dioxide micro-bubble generator 3, then introducing proportioned simulated flue gas, recording the total volume of the introduced gas as V, generating an aqueous solution containing micro-nano carbon dioxide bubbles through the device, and then introducing the aqueous solution into a reaction tank 1 to start mineralization reaction; the mechanical stirring device 2 and the ultrasonic generating device 7 arranged in the reaction tank 1 are opened to improve the mineralization reaction efficiency of the reaction tank 1.\|[0087] After the mineralized reaction material and carbon dioxide in the reaction tank 1 fully react, a filling pump 11 and a conveying control valve 13 connected with the bottom end of the reaction tank 1 are opened, and the fully mixed mineralized reaction material is conveyed to a mineralization simulation device in a paste form through a paste filling pipeline 12 by a conveying device.\|[0088] Step 5: a piezoresistive pressure sensor 16, an electromagnetic flowmeter 15 and a mineralized material sampling port 17 in the transportation device are opened, and the transportation condition of mineralized filling paste in a transportation pipeline is observed; because the system is provided with the intelligent control system, the intelligent control system is utilized to collect data online, the pressure sensor, the temperature sensor and the electromagnetic flowmeter 15 in each experimental process collect data once every 60 seconds, and the filling paste at the output port of the conveying device is sampled and analyzed through the mineralized material sampling port every 5 minutes.\|[0089] Specifically, whether the filled paste can be transported smoothly in the pipeline without blocking the pipeline is judged by analyzing the data of the pressure sensor, the temperature sensor and the electromagnetic flowmeter, and whether the filled paste still can meet the paste pumping requirement after long-time pipeline transportation is judged by analyzing the paste slump and the paste layering change value of the sample of the mineralized material sampling port 17; the transportation condition of the filling paste in the pipeline is monitored in real time through the piezoresistive pressure sensor 16 and the sampling port to observe whether the mineralized filling paste can be transported smoothly.\|[0090] Step 6: opening a sealing cover 26 on the triaxial loading device 20, conveying the conveyed mineralized filling paste to a material placing area 19 in the mineralized simulation device through a conveying pipeline, and then closing the sealing cover 26 to ensure the air tightness in the device; the gas is sampled for the first time through the gas outlet 27 on the device main body 18, the sampled gas is subjected to component analysis through an experimental instrument, analysis data are recorded, and then the gas outlet 27 is closed to ensure the gas tightness of the device.\|[0091] Specifically, the CO in the gas is obtained by sampling analysis 2 The proportion of the gas is b percent, and the gas which can chemically react with mineralized reaction materials in the simulated flue gas is mainly CO 2 The other reactive gases are of a smaller and negligible content and therefore can pass through the initial state CO 2 The ratio of the catalyst to the catalyst is a) and the residual CO in the mineralization reaction device after the reaction can be obtained 2 The content is as follows\|[0092] CO consumed by mineralization 2 The content is->\|[0093] And (3) carrying out natural maintenance on the mineralized material, and carrying out a triaxial loading test after the test block is completely solidified.\|[0094] Step 7: opening the sensor interface 28, and observing the change of the temperature and the pressure inside the device through the temperature and the pressure sensor; loading a mineralization reaction test block by simulating the stress condition of the goaf through a mineralization simulation device, and changing the temperature of the test block through an electric heating plate 24 of a forming part to simulate the temperature of a mineralization area of the goaf; the test block is subjected to a triaxial loading experiment according to the stress condition of the filled goaf by the triaxial loading device 20, and the forming environment temperature of the mineralized sample is changed by the electric heating plate 24.\|[0095] Step 8: when the pressure in the device is detected to be unchanged for a long time through the sensor, the mineralization reaction is considered to be finished, after the loading test is finished, the mineralization reaction test block is fully compressed until the gas fixed by bubbles in the test block is completely crushed and completely released, at the moment, the compression strength of the mineralization reaction test block can be obtained through the mineralization loading device, then the gas is extracted through the gas outlet 27, the gas in the device is collected for the second time, the analysis of the gas component for the second time is carried out, and the analysis result of the first component are calculated, so that the pressure-resistant strength of the mineralization reaction test block can be obtainedCO immobilized by bubbles on mineralized reaction test block 2 And (3) gas.\|[0096] The existence condition of the internal bubbles of the coagulated test block after triaxial loading test with certain strength can be judged through comparison of the two groups of data, a part of bubbles are destroyed after triaxial loading, and the internal carbon dioxide gas is dispersed, so that the gas component of the loading device is changed, and the two gas analyses can be different.\|[0097] Step 9: finally, all the gases in the mineralization simulation device are extracted through the air outlet holes 27, and the gas component analysis is carried out to obtain the content change of carbon dioxide in the gases; CO consumed by mineralization 2 Content, CO immobilized by bubbles in mineralized reaction block 2 The mineralization effect of the mineralization material is comprehensively judged by the content and the pressure bearing condition of the mineralization test block.\|[0098] Therefore, the stability of the mineralized carbon dioxide can be verified, the efficiency of the mineralized reaction for absorbing the carbon dioxide can be calculated, and the compressive strength of the mineralized test block can be obtained through the damage condition of the test block after the triaxial loading test, so that whether the mineralized filling material can well fill the goaf can be judged.\|[0099] Example III\|[0100] The embodiment provides a simulation experiment under different stress loading, and the manufacturing process and the proportion of the mineralization reaction test block of the embodiment are guaranteed to be the same as those of the embodiment one, and specifically comprises the following steps:\|[0101] step 1: weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|[0102] step 2: using dried air and analytically pure CO 2 Proportioning of simulated flue gas, recording CO 2 The percentage of the gas is set as a%;\|[0103] step 3: adding water into bubble generation equipment, then introducing proportioned simulated flue gas, recording the total volume of the introduced gas as V carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into a mineralization reaction device for mineralization reaction;\|[0104] step 4: conveying the fully mixed mineralized filling paste through a conveying device, collecting data of temperature and pressure in the system, sampling and analyzing the filling paste at an output port through a mineralized material sampling port 17, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through a pipeline monitoring device;\|[0105] step 5: the transported mineralized filling paste is transported to a mineralization simulation device through a transportation pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and the CO in the gas at the moment is obtained 2 The proportion of the gas is b percent, and the gas which can chemically react with mineralized reaction materials in the simulated flue gas is mainly CO 2 The other reactive gases are of a smaller and negligible content and therefore can pass through the initial state CO 2 The ratio of the catalyst to the catalyst is a) and the residual CO in the mineralization reaction device after the reaction can be obtained 2 The content is as follows:\|[0106] CO consumed by mineralization 2 The content is->\|[0107] And then naturally curing the mineralized material until the mineralized material is completely solidified.\|[0108] Step 6: the specific compressive strength of the test block can be known through the mineralization loading experiment of the first embodiment, the compressive strength is divided stepwise according to the compressive strength obtained in the first embodiment, the compressive strength is loaded step by step from low to high through the electrical instrument 29, and the damage degree of the test block during loading of each stage is obtained through analyzing the gas extracted from the gas outlet hole.\|[0109] Example IV\|[0110] The present example provides a secondary mineralization test under triaxial loading, and the mix ratio of mineralization reaction test blocks is the same as that of example one.\|[0111] In the solidification process of the mineralized reaction test block, simulating the stress condition of filling the goaf to carry out loading experiments on the test block, and introducing enough CO into the device in the loading process 2 Gas to mineralize reaction testThe block is subjected to secondary mineralization in loading, so that the mineralization sealing quantity is increased, the mineralization rate is improved, and the mineralization effect is enhanced.\|[0112] In mineralization reaction test block in CO 2 After the mineralization reaction is completed in the gas environment, the test block is subjected to a loading experiment again after the test block is completely solidified, the compression strength of the test block obtained by the loading experiment is compared with the compression strength of the test block obtained by the first experiment, and the degree of strengthening of the mineralization reaction by secondary mineralization is judged.\|[0113] The invention has simple and convenient simulation operation, is economical and feasible, and accords with the concept of green exploitation; by adding foaming agents such as hydrogen peroxide, aluminum powder, silica fume and the like into the mineralized reaction material, the void ratio of the mineralized material after complete reaction solidification is improved, and the filling volume is enlarged; the method comprises the steps of generating an aqueous solution containing micro-nano carbon dioxide bubbles by a micro-nano bubble generating device from carbon dioxide gas and water, introducing a mineralization reaction material to promote mineralization reaction, improving mineralization reaction rate, combining mechanical stirring and ultrasonic waves, and promoting mineralization reaction by using cavitation of ultrasonic waves and mechanical stirring.\|[0114] The transportation device adopts a sectional type transportation pipeline to simulate the transportation of mineralized filling paste on a filling site, the mineralization simulation device simulates the stress condition of a goaf to load a mineralization reaction test block, the heating device changes the temperature of the test block to simulate the temperature of a mineralization area of the goaf, and the triaxial loading device performs triaxial loading experiments on the test block in the mineralization simulation device according to the stress condition of the filling goaf, so that the test environment is ensured to be more attached to a real operation environment, and the simulation result is feasible and effective; by analyzing the gas after loading, the aim of detecting whether the mineralized filling paste can realize goaf filling is fulfilled.\|[0115] In the description of the present invention, it should be understood that the directions or positional relationships such as the terms "length", "width", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of description and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present application.\|[0116] Furthermore, in the description of the present application, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.\|[0117] The foregoing description of the preferred embodiments of the present application is not intended to be limiting, but is intended to cover any and all modifications, equivalents, and alternatives falling within the spirit and principles of the present application.	(CN116359471)\|TECHNICAL FIELD\|[0001] The invention belongs to the technical field of mineralized and sealed carbon dioxide, and particularly relates to a system and a method for dynamically simulating mineralized and sealed carbon dioxide to fill a goaf.\|BACKGROUND ART\|[0002] Carbon dioxide emission and effective treatment are the key problems of attention in various fields, and the proposal of carbon dioxide mineralization sealing gives a solution thought, wherein the carbon dioxide mineralization sealing mainly imitates and accelerates the process of rock weathering and carbon dioxide absorption in nature, carbon dioxide is dissolved in water to generate carbonic acid, then the carbonic acid reacts with alkaline minerals to generate stable solid carbonate, and the stable solid carbonate can not be decomposed in long geological years, so that the permanent sealing of the carbon dioxide can be realized.\|[0003] Because the carbon emission proportion in the coal mine industry is higher, a certain carbon fixation measure is necessary for the coal mine industry, and the mining of coal resources can cause rock stratum movement and ground surface damage, so that goafs need to be filled; the large-scale experiment is limited in site, so that the mineralization filling process of the goaf is simulated in a laboratory in a simulation mode, the practical production significance is great according to the experimental result, the mode is convenient, the economy and the feasibility are realized, and the idea of green exploitation is met.\|DISCLOSURE\|Disclosure of Invention\|[0004] The invention provides a system for dynamically simulating mineralization to seal carbon dioxide to fill a goaf, aiming at the technical problems in the prior art.\|[0005] In order to solve the technical problems, the invention comprises:\|[0006] the mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment;\|[0007] the conveying device is provided with a conveying pipeline and a pipeline monitoring device;\|[0008] and the mineralization simulation device comprises a triaxial loading device and a heating device, wherein the triaxial loading device is provided with a material supporting part and a loading assembly.\|[0009] Preferably, the reaction main body is provided with a reaction tank, a stirring device is arranged in the reaction tank, the ultrasonic generating equipment is connected with the reaction tank through a conversion device, and the bubble generating equipment is connected with a carbon dioxide gas cylinder.\|[0010] Preferably, the mineralization simulation device comprises a curing part, a loading part and a forming part, wherein the loading part is provided with a material placing area, the periphery side of the material placing area is provided with a loading pressure head and a loading baffle, and the heating equipment arranged on the forming part is arranged at the lower side of the loading part.\|[0011] The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|[0012] weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|[0013] adding water into bubble generating equipment, then introducing carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into a mineralization reaction device for mineralization reaction;\|[0014] conveying the fully mixed mineralized filling paste through a conveying device, collecting data of temperature and pressure in a system, sampling and analyzing the filling paste at an output port through a sampling port, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through a pipeline monitoring device;\|[0015] the conveyed mineralized filling paste is conveyed into a mineralization simulation device through a conveying pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and then the mineralized material is naturally cured until the mineralized material is completely solidified;\|[0016] at the moment, a triaxial loading test is carried out, a stress condition of the goaf is simulated through triaxial loading equipment, a forming environment temperature of the test block is changed through heating equipment, and the temperature of a mineralized area of the goaf is simulated;\|[0017] after the loading test is finished, extracting gas through the gas outlet hole, carrying out secondary gas component analysis, and comparing an analysis result with a primary component analysis result;\|[0018] and finally, completely extracting the gas in the mineralization simulation device through the gas outlet, analyzing the gas components to obtain the content change of carbon dioxide in the gas, and judging the mineralization effect of the mineralized material according to the numerical value change of the carbon dioxide content.\|[0019] Preferably, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 。\|[0020] Preferably, the mineralization reaction material comprises the following components in percentage by mass: 3:7:3:3.\|[0021] preferably, the mineralization reaction device is connected with the mineralization simulation device through the transportation device to form a test system, and the test system is also provided with an intelligent control system for intelligent control and data monitoring.\|[0022] Preferably, when the mineralized filling paste is conveyed by the conveying device, data acquisition is carried out on the pipeline monitoring device and monitoring equipment in the mineralization reaction device every 1 minute, sampling analysis is carried out on the filling paste at the output port of the conveying device every 5 minutes, and analysis on paste slump and paste layering change values is carried out on samples.\|[0023] Preferably, when a triaxial loading test is performed, the mineralization simulation device is heated by the heating equipment, the temperature and the pressure in the system are monitored by the detection sensor, and the mineralization is considered to be finished when the pressure in the device is kept unchanged for a long time.\|[0024] Preferably, the content of carbon dioxide fixed by bubbles in the test block after the triaxial loading test can be obtained according to the known total amount in the carbon dioxide cylinder, the content of carbon dioxide introduced into the system and the content of carbon dioxide theoretically absorbed by the mineralization reaction material, and the mineralization effect of the mineralization material can be judged according to the value.\|[0025] Compared with the prior art, the invention has the following beneficial effects:\|[0026] the invention has simple and convenient simulation operation, is economical and feasible, and accords with the concept of green exploitation; by adding foaming agents such as hydrogen peroxide, aluminum powder, silica fume and the like into the mineralized reaction material, the void ratio of the mineralized material after complete reaction solidification is improved, and the filling volume is enlarged; the method comprises the steps of generating an aqueous solution containing micro-nano carbon dioxide bubbles by a micro-nano bubble generating device from carbon dioxide gas and water, introducing a mineralization reaction material to promote mineralization reaction, improving mineralization reaction rate, combining mechanical stirring and ultrasonic waves, and promoting mineralization reaction by using cavitation of ultrasonic waves and mechanical stirring.\|[0027] The transportation device adopts a sectional type transportation pipeline to simulate the transportation of mineralized filling paste on a filling site, the mineralization simulation device simulates the stress condition of a goaf to load a mineralization reaction test block, the heating device changes the temperature of the test block to simulate the temperature of a mineralization area of the goaf, and the triaxial loading device performs triaxial loading experiments on the test block in the mineralization simulation device according to the stress condition of the filling goaf, so that the test environment is ensured to be more attached to a real operation environment, and the simulation result is feasible and effective; by analyzing the gas after loading, the aim of detecting whether the mineralized filling paste can realize goaf filling is fulfilled.\|DRAWINGS DESCRIPTION\|[0028] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are required for the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.\|[0029] FIG. 1 is a schematic structural view of a mineralization reaction device according to the present invention;\|[0030] FIG. 2 is a schematic view of a transportation device according to the present invention;\|[0031] FIG. 3 is a schematic top view of the mineralization simulator of the present invention;\|[0032] FIG. 4 is a schematic diagram of the front view of the mineralization simulator of the present invention.\|[0033] The symbol marks in the figures illustrate:\|[0034] 1. a reaction tank; 2. a mechanical stirring device; 3. a carbon dioxide microbubble generator; 4. a gas cylinder; 5. a gas control valve; 6. a flow meter; 7. an ultrasonic wave generating device; 8. an ultrasonic transducer; 9. a pressure sensor; 10. a temperature sensor; 11. a filling pump; 12. paste filling pipeline; 13. a delivery control valve; 14. mineralized material transport pipelines; 15. an electromagnetic flowmeter; 16. a piezoresistive pressure sensor; 17. a mineralized material sampling port; 18. a device body; 19. a material placement area; 20. a triaxial loading device; 21. loading an original pressure head by a triaxial; 22. triaxial loading grooving press heads; 23. loading a baffle; 24. an electric heating plate; 25. an electric hot plate controller; 26. sealing cover; 27. an air outlet hole; 28. a sensor interface; 29. an electrical method instrument.\|INVENTION MODE\|Detailed Description\|[0035] In order to make the technical problems, technical schemes and beneficial effects to be solved by the present application more clear, the present application is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the present application.\|[0036] Referring to fig. 1, the invention provides a system for dynamically simulating mineralization, sealing and carbon dioxide filling goaf, which comprises a mineralization reaction device, a transportation device and a mineralization simulation device, wherein the mineralization reaction device is connected with the mineralization simulation device through the transportation device to form a test system, and the test system is also provided with an intelligent control system, so that intelligent control and data monitoring of the system can be performed through the intelligent control system.\|[0037] The mineralization reaction device consists of a reaction main body, ultrasonic wave generating equipment and bubble generating equipment.\|[0038] Specifically, the reaction main body is provided with a reaction tank 1 for mineralizing reaction materials; a mechanical stirring device 2 is arranged in the reaction tank 1, and the mineralization reaction can be promoted to be carried out through the mechanical stirring device 2; the upper end of the reaction tank 1 is connected with bubble generating equipment arranged at the outer end through a connecting pipeline, the bubble generating equipment comprises a carbon dioxide micro-bubble generator 3 and a gas cylinder 4, the gas cylinder 4 is connected to the carbon dioxide micro-bubble generator 3, and carbon dioxide is injected into the carbon dioxide micro-bubble generator 3 through the gas cylinder 4.\|[0039] Furthermore, the bubble generating equipment is also provided with a flowmeter 6 and a gas control valve 5, and the flowmeter 6 and the gas control valve 5 are arranged on a connecting pipeline connected with the outer end of the bubble generating equipment; the bubble generating device is used for improving the mineralization reaction efficiency by introducing carbon dioxide and water into the mineralization reaction device in a micro-nano bubble mode.\|[0040] As shown in fig. 1, the lower end of the reaction tank 1 is connected with an ultrasonic generating device through a connecting line, the ultrasonic generating device comprises an ultrasonic generating device 7 and an ultrasonic transducer 8, the ultrasonic transducer 8 is fixedly arranged at the bottom of the reaction tank 1, the ultrasonic generating device 7 is connected with the reaction tank 1 through the ultrasonic transducer 8, the power of ultrasonic waves can be controlled through the ultrasonic generating device 7, the mineralization effect can be improved, and the mineralization of carbon dioxide is promoted.\|[0041] Still further, the ultrasonic wave generating means 7 may be an ultrasonic wave generator or other ultrasonic wave generating device.\|[0042] Furthermore, a pressure sensor 9 and a temperature sensor 10 are also connected to the reaction tank 1 for monitoring the reaction pressure and the reaction temperature in the reaction tank 1.\|[0043] The reaction tank 1 is provided with a mineralization reaction material conveying port through which mineralization reaction materials can be added into the reaction tank 1; the bottom end of the reaction tank 1 is connected with a filling pump 11 and a paste filling pipeline 12, so that mineralized filling paste after being fully mixed is conveyed to a conveying device for conveying through the paste filling pipeline 12, and a conveying control valve 13 is arranged on the paste filling pipeline 12 and used for controlling the conveying of the mineralized filling paste.\|[0044] As shown in fig. 2, the transportation device comprises a plurality of sectional detachable connection type mineralized material transportation pipelines 14, an electromagnetic flowmeter 15 and a piezoresistive pressure sensor 16, wherein the electromagnetic flowmeter 15 is arranged at the inlet of the mineralized material transportation pipelines 14, and a mineralized material sampling port 17 is arranged at the outlet of the mineralized material transportation pipelines 14, so that sampling and monitoring are facilitated. The transportation device simulates the pipeline transportation of mineralized materials in a mineralized filling site, and the flow condition of the mineralized materials in the pipeline is monitored in real time through the electromagnetic flowmeter 15 and the piezoresistive pressure sensor 16.\|[0045] Further, a plurality of piezoresistive pressure sensors 16 are provided at a certain distance from each other inside the mineralized material transporting pipe 14 for pressure monitoring of the paste material transported in the pipe.\|[0046] As shown in fig. 3 and 4, the mineralization simulation device is an integrated treatment device for curing, molding and loading mineralization reaction materials, and comprises a curing part, a loading part and a molding part, wherein the curing part, the loading part and the molding part are all arranged in the device main body 18; the curing part is arranged in the loading part, and when the loading test is not performed, the curing part is used for performing natural curing of the mineralized material, and the loading part is used for performing a triaxial loading test of the mineralized material.\|[0047] Specifically, the curing part is a material placing area 19 arranged at the inner side of the loading part and used for placing mineralized materials for curing and loading test; the loading part is provided with a triaxial loading device 20, the compression strength of the sample after the mineralized material is loaded, analyzed and mineralized by the triaxial loading device 20, the triaxial loading device 20 comprises a triaxial loading original pressure head 21, a triaxial loading slotted pressure head 22, a loading baffle plate 23 and an electrical instrument 29, the triaxial loading slotted pressure head 22 is arranged at the inner end of the triaxial loading original pressure head 21 and is connected through threads, and the loading pressure head and the loading baffle plate 23 are arranged at the outer peripheral side of the material placing area 19.\|[0048] The shaping portion includes electric plate 24 and electric plate controller 25, and shaping portion sets up in the below of triaxial loading device 20, heats up mineralization analogue means through the electric plate 24 of shaping portion, detects temperature change through temperature sensor after the intensification, adjusts the scope of control mineralization analogue means inside temperature to the heating element, can also change the shaping ambient temperature of test block through electric plate 24 and simulate the temperature in goaf mineralization region moreover.\|[0049] Further, as a preferred embodiment of the present invention, the electric heating plate 24 is a constant temperature graphite electric heating plate.\|[0050] Further, as a preferred embodiment of the present invention, the loading plate 23 is disposed at the inner end of the triaxial loading slot die 22, the loading plate 23 has a square plate structure, and the triaxial loading slot die 22 can abut against the loading plate 23, so that a loading force can be applied to the sample placed in the material placement region 19; and the triaxial loading device 20 is provided with a plurality of groups of loading pressure heads and loading baffles 23 which are connected in a matched manner, so that triaxial loading tests can be carried out on the samples.\|[0051] Further, the loading baffle 23 is divided into an upper part and a lower part, the lower loading baffle is arranged on the base at the lower end, and the upper loading baffle and the lower loading baffle are connected with two ends of the notch of the triaxial loading slotting pressure head 22 through threads; the triaxial loading grooving head 22 is provided with a variety of grooving dimensions, the angle being variable, and the shape and size of the loading plate 23 being variable, so as to accommodate variations in the size and inclination of the mineralised reaction material.\|[0052] Specifically, as shown in fig. 4, the upper end of the device main body 18 is further provided with a sealing cover 26 for sealing the device, so as to ensure the air tightness of the device; the sealing cover 26 is provided with an air outlet 27 and a sensor interface 28, the air inside the device is sampled and detected through the air outlet 27, the bubble stability of the mineralized sample can be judged through detection, and the sensor interface 28 can be used for connecting a temperature sensor and a pressure sensor for temperature and pressure monitoring and controlling the loading process through an electromethod instrument 29.\|[0053] Furthermore, before closing the sealing cover 26, high vacuum silicone grease is applied to the contact surface between the sealing cover 26 and the loading part arranged at the lower side to ensure the air tightness of the device.\|[0054] Example 1\|[0055] The invention also provides a method for dynamically simulating mineralization, sealing and storing carbon dioxide and filling the goaf, which comprises the following steps:\|[0056] step 1: the mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline joint of the transportation device, so that a mineralization reaction system is formed.\|[0057] Step 2: the mineralized reaction material is weighed and prepared, and is filled into a mineralized reaction device.\|[0058] Specifically, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 The composition and the optimal proportion of each part of mineralization reaction material are shown in the following table.\|[0059] TABLE 1 mineralization reaction materials composition materials and proportion table thereof\|[0060] \|[0061] The CTABs listed in table 1 are cetyltrimethylammonium bromide.\|[0062] Specifically, the filling pump 11 and the delivery control valve 13 at the bottom end of the reaction tank 1 are closed, and the prepared mineralized reaction material is added into the reaction tank 1 through the mineralized reaction material delivery port.\|[0063] Step 3: opening a gas control valve 5 and a carbon dioxide micro-bubble generator 3 of the bubble generating equipment, firstly adding a certain amount of water into the carbon dioxide micro-bubble generator 3, then introducing carbon dioxide in a gas cylinder 4 into the carbon dioxide micro-bubble generator 3, generating an aqueous solution containing micro-nano carbon dioxide bubbles through the device, and then introducing the aqueous solution into a reaction tank 1 to start mineralization reaction; the mechanical stirring device 2 and the ultrasonic generating device 7 arranged in the reaction tank 1 are opened to improve the mineralization reaction efficiency of the reaction tank 1.\|[0064] After the mineralized reaction material and carbon dioxide in the reaction tank 1 fully react, a filling pump 11 and a conveying control valve 13 connected with the bottom end of the reaction tank 1 are opened, and the fully mixed mineralized reaction material is conveyed to a mineralization simulation device in a paste form through a paste filling pipeline 12 by a conveying device.\|[0065] Step 4: a piezoresistive pressure sensor 16, an electromagnetic flowmeter 15 and a mineralized material sampling port 17 in the transportation device are opened, and the transportation condition of mineralized filling paste in a transportation pipeline is observed; because the system is provided with the intelligent control system, the intelligent control system is utilized to collect data online, the pressure sensor, the temperature sensor and the electromagnetic flowmeter 15 in each experimental process collect data once every 60 seconds, and the filling paste at the output port of the conveying device is sampled and analyzed through the mineralized material sampling port every 5 minutes.\|[0066] Specifically, whether the filled paste can be transported smoothly in the pipeline without blocking the pipeline is judged by analyzing the data of the pressure sensor, the temperature sensor and the electromagnetic flowmeter, and whether the filled paste still can meet the paste pumping requirement after long-time pipeline transportation is judged by analyzing the paste slump and the paste layering change value of the sample of the mineralized material sampling port 17; the transportation condition of the filling paste in the pipeline is monitored in real time through the piezoresistive pressure sensor 16 and the sampling port to observe whether the mineralized filling paste can be transported smoothly.\|[0067] Step 5: opening a sealing cover 26 on the triaxial loading device 20, conveying the conveyed mineralized filling paste to a material placing area 19 in the mineralized simulation device through a conveying pipeline, and then closing the sealing cover 26 to ensure the air tightness in the device; the gas is sampled for the first time through the gas outlet 27 on the device main body 18, the sampled gas is subjected to component analysis through an experimental instrument, analysis data are recorded, and then the gas outlet 27 is closed to ensure the gas tightness of the device.\|[0068] The mineralized material is naturally cured for 12 hours, after 12 hours, the test block is completely solidified, and then a triaxial loading test can be carried out.\|[0069] Step 6: opening the sensor interface 28, and observing the change of the temperature and the pressure inside the device through the temperature and the pressure sensor; loading a mineralization reaction test block by simulating the stress condition of the goaf through a mineralization simulation device, and changing the temperature of the test block through an electric heating plate 24 of a forming part to simulate the temperature of a mineralization area of the goaf; the test block is subjected to a triaxial loading experiment according to the stress condition of the filled goaf by the triaxial loading device 20, and the forming environment temperature of the mineralized sample is changed by the electric heating plate 24.\|[0070] Step 7: when the sensor detects that the pressure in the device is kept unchanged for a long time, the mineralization reaction is finished, the air outlet 27 is opened to extract the air, the air in the device is collected for the second time, the analysis of the second air component is carried out, and the analysis result is compared with the analysis result of the first component;\|[0071] the existence condition of the internal bubbles of the coagulated test block after triaxial loading test with certain strength can be judged through comparison of the two groups of data, a part of bubbles are destroyed after triaxial loading, and the internal carbon dioxide gas is dispersed, so that the gas component of the loading device is changed, and the two gas analyses can be different.\|[0072] Step 8: finally, all the gases in the mineralization simulation device are extracted through the air outlet holes 27, and the gas component analysis is carried out to obtain the content change of carbon dioxide in the gases; according to the known total amount of the carbon dioxide gas cylinder, the content of carbon dioxide gas introduced into the system and the content of carbon dioxide which can be absorbed by the mineralization reaction material in theory, the content of carbon dioxide fixed by bubbles in the test block after the triaxial loading test can be obtained, and the mineralization effect of the mineralization material can be judged by the value.\|[0073] Therefore, the stability of the mineralized carbon dioxide can be verified, the efficiency of the mineralized reaction for absorbing the carbon dioxide can be calculated, and the compressive strength of the mineralized test block can be obtained through the damage condition of the test block after the triaxial loading test, so that whether the mineralized filling material can well fill the goaf can be judged.\|[0074] Example two\|[0075] The embodiment provides a method for dynamically simulating and mineralizing and sealing carbon dioxide in flue gas to fill a goaf, which comprises the following steps:\|[0076] step 1: the mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline joint of the transportation device, so that a mineralization reaction system is formed.\|[0077] Step 2: the mineralized reaction material is weighed and prepared, and is filled into a mineralized reaction device.\|[0078] Specifically, the mineralization reaction material comprises water glass, fly ash, carbide slag, gangue and NaOH, naCl, CTAB, H 2 O 2 The composition and the optimal proportion of each part of mineralization reaction material are shown in the following table.\|[0079] TABLE 1 mineralization reaction materials composition materials and proportion table thereof\|[0080] \|[0081] The CTABs listed in table 1 are cetyltrimethylammonium bromide.\|[0082] Specifically, H 2 O 2 The CATB is a foam stabilizer.\|[0083] Specifically, the filling pump 11 and the delivery control valve 13 at the bottom end of the reaction tank 1 are closed, and the prepared mineralized reaction material is added into the reaction tank 1 through the mineralized reaction material delivery port.\|[0084] Step 3: using dried air and analytically pure CO 2 Proportioning of simulated flue gas, recording CO 2 The percentage of gas was set to a%.\|[0085] Since the composition of conventional fuel gas, fuel oil and coal flue gas is as follows: n (N) 2 :82%~89%,CO 2 :8%~15%,O 2 :3% -5%, a small amount of SO 2 Because of SO 2 The content of (C) is small, and the design is not considered, so that the dried air and pure CO for analysis are utilized 2 The composition of the flue gas can be simulated relatively accurately. (the normal air gas composition is as follows: N 2 :78%,O 2 21 percent of rare gas: 0.939%, CO 2 : 0.031), other gases and impurities: 0.03%).\|[0086] Step 4: opening a gas control valve 5 of a bubble generating device and a carbon dioxide micro-bubble generator 3, firstly adding a certain amount of water into the carbon dioxide micro-bubble generator 3, then introducing proportioned simulated flue gas, recording the total volume of the introduced gas as V, generating an aqueous solution containing micro-nano carbon dioxide bubbles through the device, and then introducing the aqueous solution into a reaction tank 1 to start mineralization reaction; the mechanical stirring device 2 and the ultrasonic generating device 7 arranged in the reaction tank 1 are opened to improve the mineralization reaction efficiency of the reaction tank 1.\|[0087] After the mineralized reaction material and carbon dioxide in the reaction tank 1 fully react, a filling pump 11 and a conveying control valve 13 connected with the bottom end of the reaction tank 1 are opened, and the fully mixed mineralized reaction material is conveyed to a mineralization simulation device in a paste form through a paste filling pipeline 12 by a conveying device.\|[0088] Step 5: a piezoresistive pressure sensor 16, an electromagnetic flowmeter 15 and a mineralized material sampling port 17 in the transportation device are opened, and the transportation condition of mineralized filling paste in a transportation pipeline is observed; because the system is provided with the intelligent control system, the intelligent control system is utilized to collect data online, the pressure sensor, the temperature sensor and the electromagnetic flowmeter 15 in each experimental process collect data once every 60 seconds, and the filling paste at the output port of the conveying device is sampled and analyzed through the mineralized material sampling port every 5 minutes.\|[0089] Specifically, whether the filled paste can be transported smoothly in the pipeline without blocking the pipeline is judged by analyzing the data of the pressure sensor, the temperature sensor and the electromagnetic flowmeter, and whether the filled paste still can meet the paste pumping requirement after long-time pipeline transportation is judged by analyzing the paste slump and the paste layering change value of the sample of the mineralized material sampling port 17; the transportation condition of the filling paste in the pipeline is monitored in real time through the piezoresistive pressure sensor 16 and the sampling port to observe whether the mineralized filling paste can be transported smoothly.\|[0090] Step 6: opening a sealing cover 26 on the triaxial loading device 20, conveying the conveyed mineralized filling paste to a material placing area 19 in the mineralized simulation device through a conveying pipeline, and then closing the sealing cover 26 to ensure the air tightness in the device; the gas is sampled for the first time through the gas outlet 27 on the device main body 18, the sampled gas is subjected to component analysis through an experimental instrument, analysis data are recorded, and then the gas outlet 27 is closed to ensure the gas tightness of the device.\|[0091] Specifically, the CO in the gas is obtained by sampling analysis 2 The proportion of the gas is b percent, and the gas which can chemically react with mineralized reaction materials in the simulated flue gas is mainly CO 2 The other reactive gases are of a smaller and negligible content and therefore can pass through the initial state CO 2 The ratio of the catalyst to the catalyst is a) and the residual CO in the mineralization reaction device after the reaction can be obtained 2 The content is as follows\|[0092] CO consumed by mineralization 2 The content is->\|[0093] And (3) carrying out natural maintenance on the mineralized material, and carrying out a triaxial loading test after the test block is completely solidified.\|[0094] Step 7: opening the sensor interface 28, and observing the change of the temperature and the pressure inside the device through the temperature and the pressure sensor; loading a mineralization reaction test block by simulating the stress condition of the goaf through a mineralization simulation device, and changing the temperature of the test block through an electric heating plate 24 of a forming part to simulate the temperature of a mineralization area of the goaf; the test block is subjected to a triaxial loading experiment according to the stress condition of the filled goaf by the triaxial loading device 20, and the forming environment temperature of the mineralized sample is changed by the electric heating plate 24.\|[0095] Step 8: when the pressure in the device is detected to be unchanged for a long time through the sensor, the mineralization reaction is considered to be finished, after the loading test is finished, the mineralization reaction test block is fully compressed until the gas fixed by bubbles in the test block is completely crushed and completely released, at the moment, the compression strength of the mineralization reaction test block can be obtained through the mineralization loading device, then the gas is extracted through the gas outlet 27, the gas in the device is collected for the second time, the analysis of the gas component for the second time is carried out, and the analysis result of the first component are calculated, so that the pressure-resistant strength of the mineralization reaction test block can be obtainedCO immobilized by bubbles on mineralized reaction test block 2 And (3) gas.\|[0096] The existence condition of the internal bubbles of the coagulated test block after triaxial loading test with certain strength can be judged through comparison of the two groups of data, a part of bubbles are destroyed after triaxial loading, and the internal carbon dioxide gas is dispersed, so that the gas component of the loading device is changed, and the two gas analyses can be different.\|[0097] Step 9: finally, all the gases in the mineralization simulation device are extracted through the air outlet holes 27, and the gas component analysis is carried out to obtain the content change of carbon dioxide in the gases; CO consumed by mineralization 2 Content, CO immobilized by bubbles in mineralized reaction block 2 The mineralization effect of the mineralization material is comprehensively judged by the content and the pressure bearing condition of the mineralization test block.\|[0098] Therefore, the stability of the mineralized carbon dioxide can be verified, the efficiency of the mineralized reaction for absorbing the carbon dioxide can be calculated, and the compressive strength of the mineralized test block can be obtained through the damage condition of the test block after the triaxial loading test, so that whether the mineralized filling material can well fill the goaf can be judged.\|[0099] Example III\|[0100] The embodiment provides a simulation experiment under different stress loading, and the manufacturing process and the proportion of the mineralization reaction test block of the embodiment are guaranteed to be the same as those of the embodiment one, and specifically comprises the following steps:\|[0101] step 1: weighing and preparing mineralized reaction materials, and loading the mineralized reaction materials into a mineralized reaction device;\|[0102] step 2: using dried air and analytically pure CO 2 Proportioning of simulated flue gas, recording CO 2 The percentage of the gas is set as a%;\|[0103] step 3: adding water into bubble generation equipment, then introducing proportioned simulated flue gas, recording the total volume of the introduced gas as V carbon dioxide, thereby generating an aqueous solution containing micro-nano carbon dioxide bubbles, and introducing the aqueous solution into a mineralization reaction device for mineralization reaction;\|[0104] step 4: conveying the fully mixed mineralized filling paste through a conveying device, collecting data of temperature and pressure in the system, sampling and analyzing the filling paste at an output port through a mineralized material sampling port 17, and monitoring the conveying condition of the mineralized filling paste in a pipeline in real time through a pipeline monitoring device;\|[0105] step 5: the transported mineralized filling paste is transported to a mineralization simulation device through a transportation pipeline, the air tightness of the mineralization simulation device is detected, the first sampling is carried out through an air outlet, the component analysis is carried out on the sampled gas, and the CO in the gas at the moment is obtained 2 The proportion of the gas is b percent, and the gas which can chemically react with mineralized reaction materials in the simulated flue gas is mainly CO 2 The other reactive gases are of a smaller and negligible content and therefore can pass through the initial state CO 2 The ratio of the catalyst to the catalyst is a) and the residual CO in the mineralization reaction device after the reaction can be obtained 2 The content is as follows:\|[0106] CO consumed by mineralization 2 The content is->\|[0107] And then naturally curing the mineralized material until the mineralized material is completely solidified.\|[0108] Step 6: the specific compressive strength of the test block can be known through the mineralization loading experiment of the first embodiment, the compressive strength is divided stepwise according to the compressive strength obtained in the first embodiment, the compressive strength is loaded step by step from low to high through the electrical instrument 29, and the damage degree of the test block during loading of each stage is obtained through analyzing the gas extracted from the gas outlet hole.\|[0109] Example IV\|[0110] The present example provides a secondary mineralization test under triaxial loading, and the mix ratio of mineralization reaction test blocks is the same as that of example one.\|[0111] In the solidification process of the mineralized reaction test block, simulating the stress condition of filling the goaf to carry out loading experiments on the test block, and introducing enough CO into the device in the loading process 2 Gas to mineralize reaction testThe block is subjected to secondary mineralization in loading, so that the mineralization sealing quantity is increased, the mineralization rate is improved, and the mineralization effect is enhanced.\|[0112] In mineralization reaction test block in CO 2 After the mineralization reaction is completed in the gas environment, the test block is subjected to a loading experiment again after the test block is completely solidified, the compression strength of the test block obtained by the loading experiment is compared with the compression strength of the test block obtained by the first experiment, and the degree of strengthening of the mineralization reaction by secondary mineralization is judged.\|[0113] The invention has simple and convenient simulation operation, is economical and feasible, and accords with the concept of green exploitation; by adding foaming agents such as hydrogen peroxide, aluminum powder, silica fume and the like into the mineralized reaction material, the void ratio of the mineralized material after complete reaction solidification is improved, and the filling volume is enlarged; the method comprises the steps of generating an aqueous solution containing micro-nano carbon dioxide bubbles by a micro-nano bubble generating device from carbon dioxide gas and water, introducing a mineralization reaction material to promote mineralization reaction, improving mineralization reaction rate, combining mechanical stirring and ultrasonic waves, and promoting mineralization reaction by using cavitation of ultrasonic waves and mechanical stirring.\|[0114] The transportation device adopts a sectional type transportation pipeline to simulate the transportation of mineralized filling paste on a filling site, the mineralization simulation device simulates the stress condition of a goaf to load a mineralization reaction test block, the heating device changes the temperature of the test block to simulate the temperature of a mineralization area of the goaf, and the triaxial loading device performs triaxial loading experiments on the test block in the mineralization simulation device according to the stress condition of the filling goaf, so that the test environment is ensured to be more attached to a real operation environment, and the simulation result is feasible and effective; by analyzing the gas after loading, the aim of detecting whether the mineralized filling paste can realize goaf filling is fulfilled.\|[0115] In the description of the present invention, it should be understood that the directions or positional relationships such as the terms "length", "width", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of description and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present application.\|[0116] Furthermore, in the description of the present application, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.\|[0117] The foregoing description of the preferred embodiments of the present application is not intended to be limiting, but is intended to cover any and all modifications, equivalents, and alternatives falling within the spirit and principles of the present application.	Family Number\|(105563865)\|105563865\|Advantages / Prev. Drawbacks\|(CN116359471 A)\|( . . . ) treatment are the key problems of attention in various fields , and the proposal of carbon dioxide mineralization sealing gives a solution thought , wherein the carbon dioxide mineralization sealing mainly imitates and accelerates the process of rock weathering and carbon dioxide absorption in nature , carbon dioxide is dissolved in water to generate carbonic acid , then the carbonic acid reacts with alkaline minerals to generate stable solid carbonate , and the stable solid carbonate can not be decomposed ( . . . ) \|Independent Claims\|(CN116359471 A)\|1. A system for dynamically simulating mineralization and sequestration of carbon dioxide filling goaf , comprising : the mineralization reaction device consists of a reaction main body , ultrasonic wave generating equipment and bubble generating equipment ; the conveying device is provided with a conveying pipeline and a pipeline ( . . . ) \|	Analysis of biological materials\|Civil engineering	E21F-015/00\|G01N-033/24		E21F-015/00\|G01N-033/24	E21F-015/00\|G01N-033/24	E21F-015/00\|G01N-033/24			CN117740754\|CN117491564\|CN117233253B\|CN116988839B	CN117740754 108978052 WHO=Examiner SELF=N CAT=A\|CN117491564 108407880 WHO=Examiner SELF=Y CAT=A\|CN117233253B 107757227 WHO=Examiner SELF=N\|CN116988839B 107136135 WHO=Examiner SELF=N	CN219910866U\|CN114673552\|US20230038447\|CN114179223\|KR20120076877	CN219910866U 107039211 WHO=Examiner SELF=Y CAT=L\|CN114673552 100630442 WHO=Examiner SELF=Y CAT=A\|US20230038447 103686458 WHO=Examiner SELF=N CAT=A\|CN114179223 99111724 WHO=Examiner SELF=N CAT=A\|KR20120076877 35305246 WHO=Examiner SELF=N CAT=A		KR20120076877; CN114179223; CN114673552; US20230038447; CN219910866U		PENDING	(CN116359471)\|PENDING	ALIVE	(CN116359471)\|ALIVE	(CN116359471)\|LEGAL DETAILS FOR CN116359471\|Actual or expected expiration date=2043-03-09\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2023-03-09\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202310241385\|Application date=2023-03-09\|Standardized application number=2023CN-0241385\|Event publication date=2023-06-30\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN116359471\|Publication stage code=A\|Publication date=2023-06-30\|Standardized publication number=CN116359471\|Event publication date=2023-06-30\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2023-07-18\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination		(CN116359471)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=hXP7Q1+dwoTq/xzSxeC8O1fn1HwLNiulWeUrB63Jy+sSjghI9dFY0TTavgWoJWcExkuDaxbg66Q=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=CN0000000068491530&ekey=2040&xpn=CN116359471&kind=A	https://pss-system.cponline.cnipa.gov.cn/conventionalSearch	https://permalink.orbit.com/RenderStaticFirstPage?XPN=6hhkKvFjdVxIIQir0tZck5NXe7dphUsu7KxJINoFg8I%3D%26n%3D1&id=0&base=FAMPAT	CN	(CN116359471)\|CN	(CN116359471)\|NAME=ANHUI UNIVERSITY OF SCIENCE & TECHNOLOGY , COUNTRY=CN		(CN116359471)\|NAME=LONG JUNBO;WEIHAI HENG YU RUN DA PATENT AGENCY OFFICE (GENERAL PARTNERSHIP) , REG=37260		(CN116359471)\|NAME=WANG CHANGXIANG\|NAME=LU YAO\|NAME=ZHOU YONGQIANG\|NAME=LU WEI\|NAME=LI JINLIANG\|NAME=LI JINHU\|NAME=ZHUO HUI\|NAME=ZHANG QINGSONG\|NAME=ZHAO SHUJIE\|NAME=LI QINGHAI\|NAME=SI LEILEI\|NAME=JIANG NING	(CN116359471)\|4	1	1					(CN116359471)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2023-06-30\|Gazette number: GAZNUM=39-2602\|Number of Pages: NPAGES=14\|		(CN116359471)\|CHINESE (CHI)	(CN116359471)\|Patent	Titre: (CN116359471)\|System and method for dynamically simulating mineralized sealed carbon dioxide filled goaf Résumé: (CN116359471)\|The invention discloses a system and method for dynamically simulating mineralized sealed carbon dioxide filled goaf, and belongs to the technical field of mineralized sealed carbon dioxide. The device is provided with a mineralization reaction device, a transportation device and a mineralization simulation device, the mineralization reaction device is composed of a reaction main body, an ultrasonic generation device and a bubble generation device, the transportation device is provided with a transportation pipeline and a pipeline monitoring device, and the mineralization simulation device comprises a triaxial loading device and a heating device. The triaxial loading equipment is provided with a material supporting part and a loading assembly. The mineralization reaction device and the mineralization simulation device are connected through the sectional type pipeline connector of the transportation device, so that the mineralization reaction system is formed, then the mineralization sealed carbon dioxide filling goaf is dynamically simulated through the mineralization reaction system, and the method is simple and convenient in simulation operation, economical and feasible and conforms to the concept of green mining.	38	Abstract	gpt-4o-mini	no	The focus is on simulating mineralized sealed carbon dioxide in goaf, not on accelerating the weathering of minerals for CO₂ capture.
38	DE102024102958	WOEP2025/052349\|DE102024102958	WO2025/163040\|DE102024102958	115032330	WO2025/163040 A1 2025-08-07 [WO2025163040]\|DE102024102958 B3 2025-06-26 [DE102024102958]	2024-02-02	2025-01-30\|2024-02-02	2025-08-07\|2025-06-26	\|(DE102024102958)\|2025-06-26	(WO2025/163040)\|2027-08-02\|(DE102024102958)\|2044-02-02	(WO2025/163040)\|Method for the thermal treatment of raw meal using an electric heating device, and corresponding system	(WO2025/163040)\|The invention relates to a method for thermally treating raw meal in order to produce burnt lime and to a corresponding system. According to the invention, raw meal is thermally treated at an electrically heated heating contact. This leads to an exhaust gas which is free of nitrous gases and other organic constituents. The pure exhaust gas can be subjected to sequestration without any further special purification processes.	KHD HUMBOLDT WEDAG	(WO2025/163040)\|KHD HUMBOLDT WEDAG GMBH ([DE])\|(DE102024102958)\|KHD Humboldt Wedag GmbH ([DE])	FEISS MARC\|KNOCH ALEXANDER\|MERSMANN MATTHIAS	(WO2025/163040)\|FEISS, Marc\|KNOCH, Alexander\|MERSMANN, Matthias		(WO2025/163040)\|In order to seal off the reactor in which the screw conveyor is arranged from the atmosphere, it is advantageously provided that the raw meal is also fed to the reactor via a star feeder. The feeding and removal of the raw meal via a cellular wheel sluice in all reactor types mentioned here has the advantage that a relatively pure exhaust gas of carbon dioxide (CO2) is produced as the exhaust gas, which only contains water (H2O) as a further constituent.\|It would be desirable to carry out the process for the thermal treatment of lime in such a way that the expensive waste gas purification before the sequestration is not necessary.\|On the other hand, the distance must also not be so small that the raw meal 10 falls through a pipeline as if it were a pipe and rolls against the gas flowing up, so that the gas and the freely trickling raw meal 10 block the path alternately.\|Since this heat does not have a very high temperature, the heat obtained from the vapors is suitable for drying other materials. The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive.\|	(WO2025/163040)\|1. Process for the thermal treatment of raw meal for the production of burnt lime, characterized by- Heating the raw meal (10) on an electrically heated heating contact. \|	(WO2025/163040)\|The aim of the invention is therefore to provide a method for thermally treating lime, in which exhaust gas purification prior to sequestration of the carbon dioxide (CO2) can be dispensed with. The object according to the invention is achieved in that the raw meal is heated on an electrically heated heating contact.\|The invention relates to a method for the thermal treatment of raw meal for producing burnt lime and a corresponding installation.\|The invention relates to a method for thermally treating raw meal in order to produce burnt lime and to a corresponding system.\|	(WO2025/163040)\|RAW MEAL(100,55)\|BURNT LIME(100,13)\|RAW MEAL TREATMENT(100,12)\|ELECTRIC HEATING(100,10)\|BURNT LIME PRODUCTION(100,2)\|TREATING RAW MEAL(60,1)\|BURNING RAW MEAL(56,1)\|LIME MEAL(48,1)\|RAW MEAL REMOVAL(41,1)\|CELLULAR WHEEL SLUICE(39,10)\|STAR FEEDER(35,2)\|SEQUESTRATION(32,11)\|REACTOR(31,30)\|TUBULAR REACTOR(27,5)\|ORGANIC COMPONENT(27,1)\|PRODUCING BURNT LIME(27,1)\|UNDULATING GAP(26,1)\|LIME TREATMENT(24,3)\|ELECTRICALLY HEATED HEATING CONTACT(23,19)\|EXPENSIVE WASTE GAS PURIFICATION(23,1)\|DUST SEPARATOR(22,6)\|PIPELINE(22,1)\|WASTE GAS PURIFICATION(22,1)\|HEAT(20,20)\|NITROUS GAS(18,3)\|EXHAUST GAS PURIFICATION(18,2)\|GAS PATH(16,2)\|LIME CALCINATION(15,6)\|CO2(14,17)\|SCREW CONVEYER(14,6)\|CALCINED RAW MEAL(14,3)\|SILICATE(14,3)\|INCLINED ARRANGEMENT(14,1)\|EXHAUST GAS(13,19)\|CARBON DIOXIDE EXHAUST GAS(13,1)\|PURIFICATION(12,1)\|ROCK(11,3)\|CASCADE(11,2)\|LIME THERMOLYSIS(11,2)\|ANOTHERSLIDING SURFACE(11,1)\|CYCLONE SEPARATOR(10,8)\|HORIZONTAL ARRANGEMENT(10,2)\|CARBON DIOXIDE(9,17)\|HEAT CONTACT(9,5)\|TREATMENT FLOW(9,2)\|RAW MEAL TURBULENCE(9,1)\|ABRASIVE RAW MEAL(8,1)\|BURNT RAW MEAL(8,1)\|VAPOR CELLULAR WHEEL SLUICE(8,1)\|BURNT PRODUCT(7,3)\|GAS COUNTERCURRENT(7,3)\|HEAT EXCHANGER(7,3)\|RAW FLOUR(7,2)\|SUSPENDED RAW MEAL(7,1)\|CLOUD SYMBOL(6,1)\|COUNTERCURRENT REACTOR(6,1)\|GRIND LIME(6,1)\|INSTALLATION REFINEMENT(6,1)\|RAW MEAL FLOWING(6,1)\|RAW MEAL HEATING(6,1)\|RAW MEAL SLIDE(6,1)\|CALCINATION PRODUCT(5,3)\|BURNED LIME(5,1)\|ENTRAIN BED REACTOR(5,1)\|FLAME PROJECT(5,1)\|PERMANENT DEPOSIT(5,1)\|SLIDE OVER(5,1)\|SLIDING OVER(5,1)\|FOOT(4,4)\|ROTARY VALVE(4,3)\|ELECTRICAL HEATING HEAT(4,2)\|DOWNSTREAM ROTARY KILN(4,1)\|GROUND LIME(4,1)\|INORGANIC BINDER(4,1)\|NATURAL DEPOSIT(4,1)\|NATURAL LIME(4,1)\|REACTOR 105(3,4)\|REGULATING FLOW(3,3)\|APPENDIX(3,1)\|AQUIFER(3,1)\|CAVERN(3,1)\|CELLULAR WHEEL LOCK(3,1)\|CEMENT CLINKER(3,1)\|\|(DE102024102958)\|RAW MEAL(100,35)\|REACTOR(100,19)\|HEAT(100,16)\|BURNT LIME(100,12)\|ELECTRICALLY HEATED HEATING CONTACT(100,11)\|RAW MEAL TREATMENT(100,8)\|ELECTRIC HEATING(100,6)\|BURNT LIME PRODUCTION(100,3)\|HEAT CONTACT(100,3)\|PLANT(100,3)\|SLIDE OVER(100,2)\|RAW MEAL FLOUR(77,1)\|BURNING RAW MEAL(57,1)\|LIME MEAL(49,1)\|RAW FLOUR(40,2)\|PRODUCING BURNT LIME(36,1)\|SEQUESTRATION(30,6)\|UNDULATING GAP(27,1)\|CASCADE(26,3)\|SLIDING SURFACE(25,24)\|EXPENSIVE WASTE GAS PURIFICATION(24,1)\|DUST SEPARATOR(23,3)\|EXHAUST GAS PURIFICATION(23,1)\|PIPELINE(23,1)\|WASTE GAS PURIFICATION(23,1)\|OFFSET ARRANGEMENT(22,1)\|TREATMENT FLOW(20,3)\|CELLULAR WHEEL SLUICE(15,4)\|LIME CALCINATION(14,5)\|SILICATE(14,3)\|ROCK(12,3)\|LIME THERMOLYSIS(11,2)\|SLIDING OVER(11,2)\|GAS PATH(11,1)\|CO2(10,4)\|HEAT EXCHANGER(10,3)\|ELECTRICALLY HEATED SLIDING SURFACE(9,4)\|HEATING213ROTARY LOCK214FLOW(9,1)\|RAW MEAL TRICKLING(9,1)\|GAS COUNTERCURRENT(7,3)\|CALCINED12RAW MEAL(7,1)\|INTERNET PUBLICATION HTTP(7,1)\|SUSPENDED RAW MEAL(7,1)\|UNBURNT11RAW MEAL(7,1)\|CARBON DIOXIDE(6,10)\|BURNING LIMESTONE(6,1)\|COUNTERCURRENT REACTOR(6,1)\|GRIND LIME(6,1)\|INSTALLATION REFINEMENT(6,1)\|RAW MEAL HEATING(6,1)\|RAW MEAL SLIDE(6,1)\|BURNT PRODUCT(5,2)\|NITROUS GAS(5,2)\|BURNED LIME(5,1)\|ENTRAIN BED REACTOR(5,1)\|FLAME PROJECT(5,1)\|CALCINATION PRODUCT(4,2)\|COMPRESSOR(4,2)\|CYCLONE SEPARATOR(4,2)\|ELECTRICAL HEATING HEAT(4,2)\|DOWNSTREAM ROTARY KILN(4,1)\|GROUND LIME(4,1)\|HEATING313ROTARY(4,1)\|INORGANIC BINDER(4,1)\|NATURAL DEPOSIT(4,1)\|NATURAL LIME(4,1)\|ROOF AREA(3,3)\|ARCHIVE(3,1)\|CEMENT CLINKER(3,1)\|CLIMATE(3,1)\|ELECTRICAL FIRE(3,1)\|	(WO2025/163040)\|P A T E N T A N S P R U C H E \|1. Process for the thermal treatment of raw meal for the production of burnt lime, characterized by\|- Heating the raw meal (10) on an electrically heated heating contact. \|2. Plant (100, 200, 300, 400) for carrying out the process according to Claim 1, having a reactor (105, 205, 305, 405) within which the electrically heated heating contact is arranged, which is designed such that the raw meal (10) slides over the electrically heated heating contact.\|3. An installation according to claim 2, characterized in that the electrically heated heating contact consists of a plurality of electrically heated heating contacts arranged vertically one above the other and offset in pairs relative to one another\|Sliding surfaces (110) exist, so that the raw meal (10) slides from top to top, as if via cascades, between the sliding surfaces (110) arranged in pairs, the sliding surfaces (110) being arranged in the reactor (105). \|4. Plant according to Claim 3, characterized in that the sliding surfaces (210) have openings through which gas produced during the thermal treatment flows and additionally heats the raw meal (10) sliding over the sliding surfaces (210).\|5. An installation according to claim 4, characterized in that the electrically heated heating contact consists of a plurality of vertically arranged and wave-shaped sliding surfaces (310) which are arranged parallel to one another and form an undulating gap in pairs between them.\|6. Plant according to claim 2, characterized in that the reactor (405) is tubular and the electrically heated heating contact is embedded in the bottom of the tubular reactor (405), the tubular reactor (405) having a horizontal or inclined arrangement, within which a screw conveyor (450) is arranged which moves the raw meal (10) over the electrically heated heating contact.\|7. Plant according to one of Claims 2 to 6, characterized in that the reactor (105, 205, 305, 405) has at least one discharge opening for the vapors produced during the thermal treatment, which discharge opening is connected to a dust separator (212, 312, 412) which separates raw meal (10) from the vapors.\|8. Plant according to Claim 7, characterized in that a heat exchanger (102) is arranged in the gas path and dissipates heat from the vapors (115) emerging from the gas paths.	(WO2025/163040)\|[0001] Process for the thermal treatment of raw meal using an electric heating device and corresponding installation \| [0002] The invention relates to a method for the thermal treatment of raw meal for producing burnt lime and a corresponding installation.\| [0003] For the production of burnt lime (CaO), it is known to grind lime (CaCOs) from natural deposits finely into so-called raw meal and to dry it suspended in a gas stream and to supply it to a thermal treatment. Burned lime (CaO) is, in addition to other substances, a starting material for the production of cement clinker, but also for the production of soda. Lime burnt is also used as a base in various chemical processes and is used in inorganic binders. Ground calcined lime is named differently depending on the industry. In the cement industry, a flour of a mixture of burnt lime and silicate-containing rock is called "raw flour". In other sectors, the pure burnt lime is also referred to as 'raw meal'. For the firing, i.e. thermal treatment of lime (CaCOs) in the form of raw meal, as a rule a flue-flow reactor is used into which a flame projects or, depending on the further process control, hot exhaust gases from a downstream rotary kiln are passed. In this thermal treatment, not only is carbon dioxide (CO2) formally driven out of the natural lime (CaCOs), which is an endothermic process, but because of the high activation energy, a comparatively high temperature of about 800°C is necessary in order to initiate the thermolysis of the lime (CaCOs). In order to generate the high temperature, it is necessary to burn fuel, the flame passing into the entrained-bed reactor. The exhaust gases from the calcination process that takes place contain carbon dioxide (CO2) from the burnt lime (CaCOs) and also carbon dioxide (CO2) from the combustion of fossil fuels. In addition to carbon dioxide (CO2), the exhaust gas also contains nitrous gases (NOx) and other exhaust gas constituents, such as volatile organic compounds (VOCs). In order to sequester the carbon dioxide (CO2) from the exhaust gas, which is recognized as harmful to the climate, it is necessary to subject the exhaust gas to a purification in order to separate air nitrogen (N2), the nitrous gases and the VOC from the exhaust gas before sequestration. \| [0004] It would be desirable to carry out the process for the thermal treatment of lime in such a way that the expensive waste gas purification before the sequestration is not necessary. \| [0005] The aim of the invention is therefore to provide a method for thermally treating lime, in which exhaust gas purification prior to sequestration of the carbon dioxide (CO2) can be dispensed with. \| [0006] The object according to the invention is achieved in that the raw meal is heated on an electrically heated heating contact. The installation corresponding thereto has a reactor within which the electrically heated heating contact is arranged, which is designed such that the raw meal slides over the electrically heated heating contact. Further advantageous embodiments of the installation are specified in the subclaims to claim 2. \| [0007] According to the idea of the invention, it is therefore provided that the raw meal, irrespective of whether it is mixed with silicate-containing rock, as is customary in the cement industry, or whether the raw meal is present as pure ground lime, is heated on an electrically heated heating contact. In order to transfer the necessary amount of heat to the raw meal, it may be advantageous in a refinement of the installation according to the invention that the speed at which the raw meal is guided past the electrically heated heating contact is slowed down by a structural arrangement of sliding surfaces as electrically heated heating contact. For this purpose, in a first embodiment of the installation according to the invention, it can be provided that the electrically heated heating contact consists of a plurality of electrically heated sliding surfaces which are arranged vertically one above the other and offset in pairs relative to one another, so that the raw meal slides from top to bottom, as via cascades, between the sliding surfaces arranged in pairs, the sliding surfaces being arranged in the reactor. The plurality of electrically heated sliding surfaces, which are arranged in pairs offset with respect to one another and vertically one above the other, behave like baffles which slow down the flow of raw meal when the raw meal trickles over the sliding surfaces from top to bottom. \| [0008] In a further embodiment of the installation according to the invention, it can be provided that the sliding surfaces have openings through which gas produced during the thermal treatment flows and additionally heats the raw meal sliding over the sliding surfaces. The openings are open to the side and in the direction of the sliding raw meal, so that the raw meal does not fall through the openings. However, the gas, which comes from below, flows through the openings and thus also flows through the sliding raw meal. During this mixing, heat which is present in the gas is transferred to the raw meal, so that it is additionally heated. The flow of the hot exhaust gases of the thermal treatment at lower stages of the electrically heated heating contact thus means a recuperation of the heat electrically introduced into the raw meal. \| [0009] In a further embodiment of the installation according to the invention, it can be provided that the electrically heated heating contact consists of a plurality of vertically arranged and wave-shaped sliding surfaces which are arranged parallel to one another. The wave-shaped sliding surfaces have a similar effect to the aforementioned sliding surfaces arranged in pairs offset relative to one another. However, the undulating sliding surfaces are arranged so close to one another that a mixture of trickling of the raw meal and turbulence of the raw meal due to gas flowing up from below, which is produced during the thermal treatment, is established in the path forming between two undulating sliding surfaces and snaking in the vertical direction. \| [0010] In yet a further embodiment of the plant according to the invention, it can be provided that the reactor is tubular and the electrically heated heating contact is embedded in the bottom of the tubular reactor, the tubular reactor having a horizontal or oblique arrangement, within which a screw conveyor is arranged. The screw conveyor moves the raw meal over the electrically heated heating contact until the burnt raw meal is ejected at the end of the reactor via a cellular wheel sluice. In order to seal off the reactor in which the screw conveyor is arranged from the atmosphere, it is advantageously provided that the raw meal is also fed to the reactor via a star feeder. The feeding and removal of the raw meal via a cellular wheel sluice in all reactor types mentioned here has the advantage that a relatively pure exhaust gas of carbon dioxide (CO2) is produced as the exhaust gas, which only contains water (H2O) as a further constituent. Since the water can easily be condensed out, the waste gas obtained in this way is suitable for sequestration, for example by storage in aquifers or in caverns as permanent deposits. \| [0011] All reactor types presented here have a vapor outlet. However, the vapors, which consist essentially of carbon dioxide (CO2) and water (H2O), still contain suspended raw meal. The suspended raw meal can be separated in a cyclone separator. The exhaust gas emerging from the cyclone separator can furthermore be passed through a heat exchanger in order to remove the heat from the vapors as process heat. Since this heat does not have a very high temperature, the heat obtained from the vapors is suitable for drying other materials. \| [0012] The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive. If, however, electrical energy can be obtained from process heat elsewhere or from renewable energies, then electrical firing in conjunction with a necessary sequestration of the carbon dioxide (CO2) produced during firing is a variant which is also entirely attractive from an economic point of view and from a climate-related point of view. \| [0013] The invention is explained in more detail with reference to the following figures. It shows: \| [0014] FIG. 1 shows an installation for the thermal treatment of raw meal using an electric heating device in a first embodiment, \| [0015] FIG. 2 shows an installation for the thermal treatment of raw meal using an electric heating device in a second embodiment, \| [0016] FIG. 3 shows an installation for the thermal treatment of raw meal using an electric heating device in a third embodiment, \| [0017] FIG. 4 shows a plant for the thermal treatment of raw meal using an electric heating device in a fourth embodiment. \| [0018] FIG. 1 shows a first embodiment of an installation 100 for the thermal treatment of raw meal 10 using an electric heating device. Raw meal 10 is passed via a cellular wheel sluice 101 into a reactor 105, where the raw meal 10 trickles over a plurality of electrically heated sliding surfaces 110 which are arranged vertically one above the other and offset with respect to one another in pairs. The sliding surfaces 110 are provided on the rear side, that is to say on the underside, with an electrical resistance heater 111 which heats the sliding surfaces 110. The sliding surfaces 110 serve to protect the resistance heater 111 present thereunder, so that the abrasive raw meal does not close the resistance heaters 111. In this embodiment, the reactor 105 is designed to be gas-tight. Vapors 115 and carbon dioxide (CO2), both of which are formed during the electric burning of the lime (CaCOs), leave the reactor 105 together with the burnt or calcined raw meal 11 at the lower foot 106 of the reactor 105 and are passed into a cyclone separator 107. In the cyclone separator 107, the burnt or calcined raw meal 11 is separated from the vapors and the carbon dioxide (CO2). The finished product, i.e. the fired or calcined raw meal 11, leaves the cyclone separator 107 at its lower coarse material outlet 108. The gas, i.e. the vapors and the carbon dioxide (CO2) leave the cyclone separator 107 at its upper fines/gas outlet 109. The gas discharged there is purified again by a dust separator 112, still fine, burnt raw meal 12 being separated off. The purified exhaust gas, the vapors 115 and the carbon dioxide (CO2) are then discarded via a flow regulator 114 and a compressor 116 for extraction for sequestration. The cloud symbol shown here for the vapors 115 is not intended to mean that the exhaust gas is discarded into the atmosphere, but rather the exhaust gas is to be subjected to sequestration, not shown in detail here. The fractions of the finished product, namely the burnt or calcined lime 11, 12, are combined and fed to further use. \| [0019] FIG. 2 shows a second embodiment of an installation 200 for the thermal treatment of raw meal 10 using an electric heating device. The installation 200 differs from the embodiment shown in FIG. 1 in that the sliding surfaces 210 have openings through which vapors 215 and carbon dioxide (CO2), both of which are produced on the lower sliding surfaces 210, can flow through the respective upper sliding surfaces 210. In this case, the exhaust gas, namely the hot vapors 215 and the hot carbon dioxide (CO2), flows through the raw meal 10 on the respective upper sliding surfaces 210, as a result of which the raw meal flowing there is additionally heated. This additional heating of the raw meal 10 means a recuperation of the waste heat which is produced at the temperature necessary for the thermolysis of the lime (CaCO3) to burnt lime (CaO). In order that the raw meal does not fall through the openings, the openings are provided with a partial compartment surface D in the sliding direction. This partial roof area D is shown more clearly in the enlarged representation of the detail A. The partial roof area D is shown in FIGS. Unlike the reactor 105 in the embodiment in FIG. 1, the reactor 205 shown here is provided with a gas opening at the head 204 of the reactor 205 with a gas outlet. This arrangement of a gas outlet leads to a gas countercurrent within the reactor 205, which is represented by vertical arrows drawn in the reactor 205. The gas flows upwards into the gas discharge in the head 204 of the reactor 205, whereas the completely burnt or calcined product falls into the foot 206 of the reactor 205. There the completely burnt or calcined lime is discharged through a cellular wheel sluice 213. The burnt or calcined lime 11 separated in the dust separator 207 is combined with the product originating from the cellular wheel sluice 213. The exhaust gas, on the other hand, flows via a flow regulator 214 and compressor 216 to its further sequestration. \| [0020] FIG. 3 shows an installation 300 for the thermal treatment of raw meal 10 using an electric heating device in a third embodiment. In contrast to the cascade-like sliding surfaces 110 and 210 in the two embodiments mentioned above, it is provided in this embodiment that the sliding surfaces 310 are sliding surfaces 310 which are in the form of electrically heated heating contacts, are close to one another and have a wavy construction and between them form a sinuous or undulating gap extending essentially from top to bottom. Within the gap between two sliding surfaces 310, a mixing movement is formed from a trickling of the raw meal 10 and a gas countercurrent, in which the raw meal 10, which is present with the already partially burnt or calcined lime 11, is swirled up in a manner similar to that in a countercurrent reactor. The gas countercurrent has a heat-recuperating effect which has already been discussed with respect to the embodiment of the plant in FIG. 2. It is important here that the distance between the second sliding surfaces 310 is not too wide, so that a separation between the trickling of the raw meal and the upward flow of the exhaust gas cannot occur. On the other hand, the distance must also not be so small that the raw meal 10 falls through a pipeline as if it were a pipe and rolls against the gas flowing up, so that the gas and the freely trickling raw meal 10 block the path alternately. The sliding surfaces 310 are connected on one side to resistance heaters 311. The gas flows upwards into the gas discharge in the head 304 of the reactor 305, whereas the completely burnt or calcined product falls into the foot 306 of the reactor 305. There the completely burnt or calcined lime is discharged through a cellular wheel sluice 313. The burnt or calcined lime 11 separated in the dust separator 307 is combined with the product originating from the cellular wheel sluice 313. The exhaust gas, on the other hand, flows via a flow regulator 314 and compressor 2316 to its further sequestration. \| [0021] Finally, FIG. 4 shows an installation 400 for the thermal treatment of raw meal 10 using an electric heating device 410 in a fourth embodiment. A screw conveyor 450 is arranged in the reactor 405, which is shown as a tubular reactor 405 horizontally or obliquely ("obliquely" not shown here). This screw conveyor 450 transports the raw meal 10 introduced into the reactor 405 via a cellular wheel sluice 401 via the sliding surfaces 410 which are let into the lower wall 451 and are electrically heated from below by resistance heaters 411. This embodiment has the advantage that the dwell time of the raw meal 10 on the sliding surfaces 410 can be set as an electrically heated heating contact with the speed of the screw conveyor 450. Vapors 415 and carbon dioxide (CO2) are also produced as waste gas in this reactor 405. This exhaust gas is passed via gas discharge lines 460 to a dust separator 412 which separates raw meal 11 still suspended in the exhaust gas from the exhaust gas. The remaining exhaust gas from vapors 415 and carbon dioxide (CO2) is then subjected to sequestration. On the other hand, the completely burnt or calcined product from the cellular wheel sluice is combined with the separated product from the dust separator 412.\| [0022] B E Z U G S Z E I C H E N L I S E \| [0023] Raw meal, unburnt 200 plant\| [0024] Raw flour, calcined 201 star feeder\| [0025] Raw meal, calcined 204 head (reactor) \| [0026] 205 Reactor\| [0027] Appendix 206 feet (reactor)\| [0028] Rotary valve 207 cyclone separator\| [0029] Heat exchanger 208 coarse material discharge\| [0030] Reactor 209 fines/gas outlet\| [0031] Foot (reactor) 210 sliding surface\| [0032] Cyclone separator 211 resistance heating\| [0033] Coarse material outlet 213 rotary valve\| [0034] Fine/gas outlet 214 flow controller\| [0035] Sliding surface 215 vapors\| [0036] Resistance heating 216 Compressor\| [0037] dust collector \| [0038] Cellular wheel lock 300 system\| [0039] Flow controller 301 rotary valve\| [0040] Vapors 304 head (reactor)\| [0041] Compressor 305 reactor \| [0042] 306 feet (reactor) sliding surface 414 flow regulator resistance heater 415 vapors cellular wheel sluice 416 compressor flow regulator 450 screw conveyor vapors 451 wall compressor 460 gas discharge system A detail cellular wheel sluice D partial roof surface dust separator	(WO2025/163040)\|[0001] Process for the thermal treatment of raw meal using an electric heating device and corresponding installation \| [0002] The invention relates to a method for the thermal treatment of raw meal for producing burnt lime and a corresponding installation.\| [0003] For the production of burnt lime (CaO), it is known to grind lime (CaCOs) from natural deposits finely into so-called raw meal and to dry it suspended in a gas stream and to supply it to a thermal treatment. Burned lime (CaO) is, in addition to other substances, a starting material for the production of cement clinker, but also for the production of soda. Lime burnt is also used as a base in various chemical processes and is used in inorganic binders. Ground calcined lime is named differently depending on the industry. In the cement industry, a flour of a mixture of burnt lime and silicate-containing rock is called "raw flour". In other sectors, the pure burnt lime is also referred to as 'raw meal'. For the firing, i.e. thermal treatment of lime (CaCOs) in the form of raw meal, as a rule a flue-flow reactor is used into which a flame projects or, depending on the further process control, hot exhaust gases from a downstream rotary kiln are passed. In this thermal treatment, not only is carbon dioxide (CO2) formally driven out of the natural lime (CaCOs), which is an endothermic process, but because of the high activation energy, a comparatively high temperature of about 800°C is necessary in order to initiate the thermolysis of the lime (CaCOs). In order to generate the high temperature, it is necessary to burn fuel, the flame passing into the entrained-bed reactor. The exhaust gases from the calcination process that takes place contain carbon dioxide (CO2) from the burnt lime (CaCOs) and also carbon dioxide (CO2) from the combustion of fossil fuels. In addition to carbon dioxide (CO2), the exhaust gas also contains nitrous gases (NOx) and other exhaust gas constituents, such as volatile organic compounds (VOCs). In order to sequester the carbon dioxide (CO2) from the exhaust gas, which is recognized as harmful to the climate, it is necessary to subject the exhaust gas to a purification in order to separate air nitrogen (N2), the nitrous gases and the VOC from the exhaust gas before sequestration. \| [0004] It would be desirable to carry out the process for the thermal treatment of lime in such a way that the expensive waste gas purification before the sequestration is not necessary. \| [0005] The aim of the invention is therefore to provide a method for thermally treating lime, in which exhaust gas purification prior to sequestration of the carbon dioxide (CO2) can be dispensed with. \| [0006] The object according to the invention is achieved in that the raw meal is heated on an electrically heated heating contact. The installation corresponding thereto has a reactor within which the electrically heated heating contact is arranged, which is designed such that the raw meal slides over the electrically heated heating contact. Further advantageous embodiments of the installation are specified in the subclaims to claim 2. \| [0007] According to the idea of the invention, it is therefore provided that the raw meal, irrespective of whether it is mixed with silicate-containing rock, as is customary in the cement industry, or whether the raw meal is present as pure ground lime, is heated on an electrically heated heating contact. In order to transfer the necessary amount of heat to the raw meal, it may be advantageous in a refinement of the installation according to the invention that the speed at which the raw meal is guided past the electrically heated heating contact is slowed down by a structural arrangement of sliding surfaces as electrically heated heating contact. For this purpose, in a first embodiment of the installation according to the invention, it can be provided that the electrically heated heating contact consists of a plurality of electrically heated sliding surfaces which are arranged vertically one above the other and offset in pairs relative to one another, so that the raw meal slides from top to bottom, as via cascades, between the sliding surfaces arranged in pairs, the sliding surfaces being arranged in the reactor. The plurality of electrically heated sliding surfaces, which are arranged in pairs offset with respect to one another and vertically one above the other, behave like baffles which slow down the flow of raw meal when the raw meal trickles over the sliding surfaces from top to bottom. \| [0008] In a further embodiment of the installation according to the invention, it can be provided that the sliding surfaces have openings through which gas produced during the thermal treatment flows and additionally heats the raw meal sliding over the sliding surfaces. The openings are open to the side and in the direction of the sliding raw meal, so that the raw meal does not fall through the openings. However, the gas, which comes from below, flows through the openings and thus also flows through the sliding raw meal. During this mixing, heat which is present in the gas is transferred to the raw meal, so that it is additionally heated. The flow of the hot exhaust gases of the thermal treatment at lower stages of the electrically heated heating contact thus means a recuperation of the heat electrically introduced into the raw meal. \| [0009] In a further embodiment of the installation according to the invention, it can be provided that the electrically heated heating contact consists of a plurality of vertically arranged and wave-shaped sliding surfaces which are arranged parallel to one another. The wave-shaped sliding surfaces have a similar effect to the aforementioned sliding surfaces arranged in pairs offset relative to one another. However, the undulating sliding surfaces are arranged so close to one another that a mixture of trickling of the raw meal and turbulence of the raw meal due to gas flowing up from below, which is produced during the thermal treatment, is established in the path forming between two undulating sliding surfaces and snaking in the vertical direction. \| [0010] In yet a further embodiment of the plant according to the invention, it can be provided that the reactor is tubular and the electrically heated heating contact is embedded in the bottom of the tubular reactor, the tubular reactor having a horizontal or oblique arrangement, within which a screw conveyor is arranged. The screw conveyor moves the raw meal over the electrically heated heating contact until the burnt raw meal is ejected at the end of the reactor via a cellular wheel sluice. In order to seal off the reactor in which the screw conveyor is arranged from the atmosphere, it is advantageously provided that the raw meal is also fed to the reactor via a star feeder. The feeding and removal of the raw meal via a cellular wheel sluice in all reactor types mentioned here has the advantage that a relatively pure exhaust gas of carbon dioxide (CO2) is produced as the exhaust gas, which only contains water (H2O) as a further constituent. Since the water can easily be condensed out, the waste gas obtained in this way is suitable for sequestration, for example by storage in aquifers or in caverns as permanent deposits. \| [0011] All reactor types presented here have a vapor outlet. However, the vapors, which consist essentially of carbon dioxide (CO2) and water (H2O), still contain suspended raw meal. The suspended raw meal can be separated in a cyclone separator. The exhaust gas emerging from the cyclone separator can furthermore be passed through a heat exchanger in order to remove the heat from the vapors as process heat. Since this heat does not have a very high temperature, the heat obtained from the vapors is suitable for drying other materials. \| [0012] The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive. If, however, electrical energy can be obtained from process heat elsewhere or from renewable energies, then electrical firing in conjunction with a necessary sequestration of the carbon dioxide (CO2) produced during firing is a variant which is also entirely attractive from an economic point of view and from a climate-related point of view. \| [0013] The invention is explained in more detail with reference to the following figures. It shows: \| [0014] FIG. 1 shows an installation for the thermal treatment of raw meal using an electric heating device in a first embodiment, \| [0015] FIG. 2 shows an installation for the thermal treatment of raw meal using an electric heating device in a second embodiment, \| [0016] FIG. 3 shows an installation for the thermal treatment of raw meal using an electric heating device in a third embodiment, \| [0017] FIG. 4 shows a plant for the thermal treatment of raw meal using an electric heating device in a fourth embodiment. \| [0018] FIG. 1 shows a first embodiment of an installation 100 for the thermal treatment of raw meal 10 using an electric heating device. Raw meal 10 is passed via a cellular wheel sluice 101 into a reactor 105, where the raw meal 10 trickles over a plurality of electrically heated sliding surfaces 110 which are arranged vertically one above the other and offset with respect to one another in pairs. The sliding surfaces 110 are provided on the rear side, that is to say on the underside, with an electrical resistance heater 111 which heats the sliding surfaces 110. The sliding surfaces 110 serve to protect the resistance heater 111 present thereunder, so that the abrasive raw meal does not close the resistance heaters 111. In this embodiment, the reactor 105 is designed to be gas-tight. Vapors 115 and carbon dioxide (CO2), both of which are formed during the electric burning of the lime (CaCOs), leave the reactor 105 together with the burnt or calcined raw meal 11 at the lower foot 106 of the reactor 105 and are passed into a cyclone separator 107. In the cyclone separator 107, the burnt or calcined raw meal 11 is separated from the vapors and the carbon dioxide (CO2). The finished product, i.e. the fired or calcined raw meal 11, leaves the cyclone separator 107 at its lower coarse material outlet 108. The gas, i.e. the vapors and the carbon dioxide (CO2) leave the cyclone separator 107 at its upper fines/gas outlet 109. The gas discharged there is purified again by a dust separator 112, still fine, burnt raw meal 12 being separated off. The purified exhaust gas, the vapors 115 and the carbon dioxide (CO2) are then discarded via a flow regulator 114 and a compressor 116 for extraction for sequestration. The cloud symbol shown here for the vapors 115 is not intended to mean that the exhaust gas is discarded into the atmosphere, but rather the exhaust gas is to be subjected to sequestration, not shown in detail here. The fractions of the finished product, namely the burnt or calcined lime 11, 12, are combined and fed to further use. \| [0019] FIG. 2 shows a second embodiment of an installation 200 for the thermal treatment of raw meal 10 using an electric heating device. The installation 200 differs from the embodiment shown in FIG. 1 in that the sliding surfaces 210 have openings through which vapors 215 and carbon dioxide (CO2), both of which are produced on the lower sliding surfaces 210, can flow through the respective upper sliding surfaces 210. In this case, the exhaust gas, namely the hot vapors 215 and the hot carbon dioxide (CO2), flows through the raw meal 10 on the respective upper sliding surfaces 210, as a result of which the raw meal flowing there is additionally heated. This additional heating of the raw meal 10 means a recuperation of the waste heat which is produced at the temperature necessary for the thermolysis of the lime (CaCO3) to burnt lime (CaO). In order that the raw meal does not fall through the openings, the openings are provided with a partial compartment surface D in the sliding direction. This partial roof area D is shown more clearly in the enlarged representation of the detail A. The partial roof area D is shown in FIGS. Unlike the reactor 105 in the embodiment in FIG. 1, the reactor 205 shown here is provided with a gas opening at the head 204 of the reactor 205 with a gas outlet. This arrangement of a gas outlet leads to a gas countercurrent within the reactor 205, which is represented by vertical arrows drawn in the reactor 205. The gas flows upwards into the gas discharge in the head 204 of the reactor 205, whereas the completely burnt or calcined product falls into the foot 206 of the reactor 205. There the completely burnt or calcined lime is discharged through a cellular wheel sluice 213. The burnt or calcined lime 11 separated in the dust separator 207 is combined with the product originating from the cellular wheel sluice 213. The exhaust gas, on the other hand, flows via a flow regulator 214 and compressor 216 to its further sequestration. \| [0020] FIG. 3 shows an installation 300 for the thermal treatment of raw meal 10 using an electric heating device in a third embodiment. In contrast to the cascade-like sliding surfaces 110 and 210 in the two embodiments mentioned above, it is provided in this embodiment that the sliding surfaces 310 are sliding surfaces 310 which are in the form of electrically heated heating contacts, are close to one another and have a wavy construction and between them form a sinuous or undulating gap extending essentially from top to bottom. Within the gap between two sliding surfaces 310, a mixing movement is formed from a trickling of the raw meal 10 and a gas countercurrent, in which the raw meal 10, which is present with the already partially burnt or calcined lime 11, is swirled up in a manner similar to that in a countercurrent reactor. The gas countercurrent has a heat-recuperating effect which has already been discussed with respect to the embodiment of the plant in FIG. 2. It is important here that the distance between the second sliding surfaces 310 is not too wide, so that a separation between the trickling of the raw meal and the upward flow of the exhaust gas cannot occur. On the other hand, the distance must also not be so small that the raw meal 10 falls through a pipeline as if it were a pipe and rolls against the gas flowing up, so that the gas and the freely trickling raw meal 10 block the path alternately. The sliding surfaces 310 are connected on one side to resistance heaters 311. The gas flows upwards into the gas discharge in the head 304 of the reactor 305, whereas the completely burnt or calcined product falls into the foot 306 of the reactor 305. There the completely burnt or calcined lime is discharged through a cellular wheel sluice 313. The burnt or calcined lime 11 separated in the dust separator 307 is combined with the product originating from the cellular wheel sluice 313. The exhaust gas, on the other hand, flows via a flow regulator 314 and compressor 2316 to its further sequestration. \| [0021] Finally, FIG. 4 shows an installation 400 for the thermal treatment of raw meal 10 using an electric heating device 410 in a fourth embodiment. A screw conveyor 450 is arranged in the reactor 405, which is shown as a tubular reactor 405 horizontally or obliquely ("obliquely" not shown here). This screw conveyor 450 transports the raw meal 10 introduced into the reactor 405 via a cellular wheel sluice 401 via the sliding surfaces 410 which are let into the lower wall 451 and are electrically heated from below by resistance heaters 411. This embodiment has the advantage that the dwell time of the raw meal 10 on the sliding surfaces 410 can be set as an electrically heated heating contact with the speed of the screw conveyor 450. Vapors 415 and carbon dioxide (CO2) are also produced as waste gas in this reactor 405. This exhaust gas is passed via gas discharge lines 460 to a dust separator 412 which separates raw meal 11 still suspended in the exhaust gas from the exhaust gas. The remaining exhaust gas from vapors 415 and carbon dioxide (CO2) is then subjected to sequestration. On the other hand, the completely burnt or calcined product from the cellular wheel sluice is combined with the separated product from the dust separator 412.\| [0022] B E Z U G S Z E I C H E N L I S E \| [0023] Raw meal, unburnt 200 plant\| [0024] Raw flour, calcined 201 star feeder\| [0025] Raw meal, calcined 204 head (reactor) \| [0026] 205 Reactor\| [0027] Appendix 206 feet (reactor)\| [0028] Rotary valve 207 cyclone separator\| [0029] Heat exchanger 208 coarse material discharge\| [0030] Reactor 209 fines/gas outlet\| [0031] Foot (reactor) 210 sliding surface\| [0032] Cyclone separator 211 resistance heating\| [0033] Coarse material outlet 213 rotary valve\| [0034] Fine/gas outlet 214 flow controller\| [0035] Sliding surface 215 vapors\| [0036] Resistance heating 216 Compressor\| [0037] dust collector \| [0038] Cellular wheel lock 300 system\| [0039] Flow controller 301 rotary valve\| [0040] Vapors 304 head (reactor)\| [0041] Compressor 305 reactor \| [0042] 306 feet (reactor) sliding surface 414 flow regulator resistance heater 415 vapors cellular wheel sluice 416 compressor flow regulator 450 screw conveyor vapors 451 wall compressor 460 gas discharge system A detail cellular wheel sluice D partial roof surface dust separator	Family Number\|(115032330)\|115032330\|Object of Invention\|(DE102024102958 B3)\|It is therefore the object of the invention to provide a plant for the thermal treatment of lime in which exhaust gas purification before sequestration of the carbon dioxide (CO2_) can be dispensed with.\|(WO2025163040 A1)\|The aim of the invention is therefore to provide a method for thermally treating lime, in which exhaust gas purification prior to sequestration of the carbon dioxide (CO2) can be dispensed with. \|Advantages / Prev. Drawbacks\|(DE102024102958 B3)\| (...) The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive.\|(WO2025163040 A1)\| (...) The present invention of burning raw meal electrically, whether with silicate-containing rock or as pure lime meal, initially appears to be very expensive and therefore unattractive.\|	Materials, metallurgy\|Thermal processes and apparatus	C04B-002/12\|F27B-001/08\|F27D-011/02\|F27D-099/00/06		C04B-002/12\|F27B-001/08\|F27D-011/02\|F27D-099/00/06	C04B-002/10\|C04B-002/12\|F27B-001/08\|F27D-011/02\|F27D-099/00	C04B-002/10\|C04B-002/12\|F27B-001/08\|F27D-011/02\|F27D-099/00					US20240002288\|CN113149471\|US20210231374\|CN109133676\|CN103443046B\|DE102023202994\|DE4431508	US20240002288 100489638 WHO=Examiner SELF=N CAT=X CAT=I\|CN113149471 95339649 WHO=Examiner SELF=N CAT=X\|US20210231374 86865659 WHO=Examiner SELF=N CAT=X\|CN109133676 82881447 WHO=Examiner SELF=N CAT=X\|CN103443046B 7861390 WHO=Examiner SELF=N CAT=A\|DE102023202994 111675951 WHO=Examiner SELF=N\|DE4431508 13045774 WHO=Examiner SELF=N		US20240002288; CN113149471; CN109133676; US20210231374; CN103443046B\|DE4431508; DE102023202994	\|(DE102024102958)\|Search Report references [Examiner]\|-IBU tec: Der Drehrohrofen. URL: https://www.ibu-tec.de/anlagen/drehrohrofen/ [abgerufen am 16.10.2024]; vgl. auch http://web.archive.org/web/20230810231918/https://www.ibu-tec.de/anlagen/drehrohrofen/ (archiviert am 10.08.2023)i.V.m. Kalzinierung. URL: https://www.ibu-tec.de/expertise/prozesse/kalzinierung/ [abgerufen a, 16.10.2024]; vgl. auch https://web.archive.org/web/20231202013009/https://www.ibu-tec.de/expertise/prozesse/kalzinierung/ (archiviert am 02.12.2023)\|	GRANTED	(WO2025/163040)\|PENDING\|(DE102024102958)\|GRANTED	ALIVE	(WO2025/163040)\|ALIVE\|(DE102024102958)\|ALIVE	(WO2025/163040)\|LEGAL DETAILS FOR WO2025/163040\|Actual or expected expiration date=2027-08-02\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-01-30\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOEP2025/052349\|Application date=2025-01-30\|Standardized application number=2025WO-EP52349\|Event publication date=2025-08-07\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2025/163040\|Publication stage code=A1\|Publication date=2025-08-07\|Standardized publication number=WO2025163040\|MEMBER STATE LEGAL DETAILS FOR EP\|Actual or expected expiration date=2045-01-30\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP25702812\|Event publication date=2025-09-17\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|(DE102024102958)\|LEGAL DETAILS FOR DE102024102958\|Actual or expected expiration date=2044-02-02\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2024-02-02\|Event code=DE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=DE DE102024102958\|Application date=2024-02-02\|Standardized application number=2024DE-10102958\|Event publication date=2024-02-02\|Event code=DE/R012\|Event indicator=Pos\|Event group=Examination events\|Request for examination validly filed\|Pruefungsantrag wirksam gestellt\|Event publication date=2025-02-24\|Event code=DE/R016\|Event group=Examination events\|Response to examination communication\|Erwiderung auf pruefungsbescheid\|Event publication date=2025-03-17\|Event code=DE/R018\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant decision by examination section/examining division\|Erteilungsbeschluss durch pruefungsstelle/patentabteilung\|Event publication date=2025-06-26\|Event code=DE/B3\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent (First publication)\|Publication country=DE\|Publication number=DE102024102958\|Publication stage code=B3\|Publication date=2025-06-26\|Standardized publication number=DE102024102958	(WO2025/163040)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2025/163040)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2025/163040)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, ME, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2025/163040)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2025/163040)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, MG, EC, MK, US, EE, MN, EG, UY, UZ, MU, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(WO2025/163040)\|WO; EP\|(DE102024102958)\|DE	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=icjTorqguCCYFl50vavvmN0P/F2Pwh1EkaV0SMUACwOCCKReMmHu7M9Ry4MrhQjLALkMBz8hwaI=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=WO0000000006833387&ekey=2608&xpn=WO2025163040&kind=A1	http://www.wipo.int/patentscope/search/en/detail.jsf?docId=WO2025163040&redirectedID=true	https://permalink.orbit.com/RenderStaticFirstPage?XPN=C8Srd52QghD6%252FxdSEPJ%252FabmsLuw%252FR4oY%252BQgpgFzVRnM%3D%26n%3D1&id=0&base=FAMPAT	DE	(WO2025/163040)\|DE\|(DE102024102958)\|DE	(WO2025/163040)\|NAME=KHD HUMBOLDT WEDAG GMBH Von-der-Wettern-Straße 4a 51149 Köln , COUNTRY=DE\|(DE102024102958)\|NAME=KHD Humboldt Wedag GmbH , CITY=Köln , POSTCODE=51067 , COUNTRY=DE			(WO2025/163040)\|DE; DE; DE\|(DE102024102958)\|DE; DE; DE	(WO2025/163040)\|NAME=FEISS, Marc Düsseldorfer Straße 125 51063 Köln, POSTCODE=51063, COUNTRY=DE \|NAME=KNOCH, Alexander Salgert 17 53797 Lohmar, POSTCODE=53797, COUNTRY=DE \|NAME=MERSMANN, Matthias Burgstraße 31 52222 Stolberg, POSTCODE=52222, COUNTRY=DE\|(DE102024102958)\|NAME=Mersmann Matthias, CITY=Stolberg, POSTCODE=52222, COUNTRY=DE \|NAME=Knoch Alexander, CITY=Lohmar, POSTCODE=53797, COUNTRY=DE \|NAME=Feiss Marc, CITY=Köln, POSTCODE=51063, COUNTRY=DE	(WO2025/163040)\|4\|(DE102024102958)\|1	1	2					(WO2025/163040)\|Number of Claims: NCL=8\|Extended kind: EXTK=x\|\|(DE102024102958)\|Number of Claims: NCL=4\|		(WO2025/163040)\|GERMAN (GER)	(WO2025163040)\|Patent\|(DE102024102958)\|Patent	Titre: (WO2025/163040)\|Method for the thermal treatment of raw meal using an electric heating device, and corresponding system Résumé: (WO2025/163040)\|The invention relates to a method for thermally treating raw meal in order to produce burnt lime and to a corresponding system. According to the invention, raw meal is thermally treated at an electrically heated heating contact. This leads to an exhaust gas which is free of nitrous gases and other organic constituents. The pure exhaust gas can be subjected to sequestration without any further special purification processes.	37	Abstract	gpt-4o-mini	no	The article focuses on thermal treatment for producing burnt lime and does not address accelerated weathering or CO₂ capture through mineral alteration.
39	EP11305696\|EP12727348\|WOEP2012/060480	WOEP2012/060480\|EP12727348\|HRP20180851T\|CN201280027687\|US14/123,987\|KR20137035129\|CA2838035\|EP11305696	HRP20180851\|EP2718230\|CN103582611\|US9469546\|US20140120022\|EP2718230\|KR10-2014-0045459\|CN103582611\|CA2838035\|WO2012/168176\|EP2532624	15065813	WO2012/168176 A1 2012-12-13 [WO2012168176]\|EP2718230 B1 2018-05-23 [EP2718230]\|EP2718230 A1 2014-04-16 [EP2718230]\|HRP20180851 T1 2018-06-29 [HRP20180851]\|CN103582611 B 2017-03-08 [CN103582611B]\|CN103582611 A 2014-02-12 [CN103582611]\|US9469546 B2 2016-10-18 [US9469546]\|US20140120022 A1 2014-05-01 [US20140120022]\|KR10-2014-0045459 A 2014-04-16 [KR20140045459]\|CA2838035 A1 2012-12-13 [CA2838035]\|EP2532624 A1 2012-12-12 [EP2532624]	2011-06-07\|2012-06-04	2012-06-04\|2012-06-04\|2012-06-04\|2012-06-04\|2012-06-04\|2012-06-04\|2012-06-04\|2011-06-07	2018-06-29\|2018-05-23\|2017-03-08\|2016-10-18\|2014-05-01\|2014-04-16\|2014-04-16\|2014-02-12\|2012-12-13\|2012-12-13\|2012-12-12	(EP2718230)\|2018-05-23\|\|(US9469546)\|2016-10-18\|\|(CN103582611B)\|2017-03-08\|(HRP20180851)\|2018-06-29\|\|	(EP2718230)\|2032-06-04\|(EP2532624)\|2017-07-15\|(US9469546)\|2020-11-23\|(WO2012/168176)\|2014-12-07\|(CN103582611)\|2019-06-04\|(HRP20180851)\|2019-06-04\|(KR10-2014-0045459)\|2017-07-05\|(CA2838035)\|2020-08-31	(EP2718230)\|Process for the mineralization of carbon dioxide	(EP2718230)\|The invention provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form, or in the form of an alkali metal carbonate or bicarbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.	HOLCIM TECHNOLOGY\|LAFARGE	(EP2718230)\|Lafarge ([FR])\|(EP2718230)\|Lafarge ([FR])\|(EP2532624)\|LAFARGE ([FR])\|(US9469546)\|LAFARGE ([FR])\|(US20140120022)\|LAFARGE ([FR])\|(WO2012/168176)\|LAFARGE ([FR])\|(CN103582611)\|LAFARGE SA ([FR])\|(CN103582611)\|LAFARGE SA ([FR])\|(HRP20180851)\|Lafarge\|(KR10-2014-0045459)\|LAFARGE\|(CA2838035)\|LAFARGE ([FR])	GARTNER ELLIS\|PISCH ALEXANDER	(EP2718230)\|GARTNER, Ellis\|PISCH, Alexander\|(EP2718230)\|GARTNER, Ellis\|PISCH, Alexander	(EP2718230)\|Keschmann, Marc;Haffner und Keschmann ([AT])\|Reg. Nb: 101393339\|(EP2532624)\|Mérigeault, Shona;Lafarge ([FR])\|Reg. Nb: 101004378\|(US9469546)\|Pillsbury Winthrop Shaw Pittman LLP\|(WO2012/168176)\|MERIGEAULT, Shona ([FR])\|(CN103582611)\|CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11314\|ZHU HUINING;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11314\|(KR10-2014-0045459)\|KOREANA PATENT FIRM\|Reg. Nb: 920011000013\|(CA2838035)\|NORTON ROSE FULBRIGHT CANADA LLP/S.E.N.C.R.L., S.R.L. ([CA])	(EP2718230)\|However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|It is therefore desirable to separate this alkali metal carbonate solution and extract the alkali metal carbonates in solid form for re-use in the high temperature process according to reaction (1).\|The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible.\|One of the major technical difficulties which renders such processes so expensive to set up and operate is the need to use elevated pressures and temperatures in order to achieve a sufficiently high rate (for industrial purposes) of carbonation of magnesium silicate minerals. Typically, the carbon dioxide gas must first be purified and then compressed to pressures in excess of 70 atmospheres, and then contacted with finely-ground magnesium silicates in a pressure reactor at temperatures of 120-200°C. This requires specialized equipment which is expensive to build and maintain, as well as large amounts of electric power to operate the gas purification and pressurization process as well as to finely grind the magnesium silicate rocks.\|	(EP2718230)\|1. A process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|	(EP2718230)\|The invention also provides a process for the preparation of a product comprising an alkali metal magnesium silicate compound (which compound is preferably of composition R2OMgOSiO2, (in which R represents an alkali metal),which process comprises the reaction, at a temperature from 500 to 1100°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 2:1 to 1:2, which reaction produces the product comprising an alkali metal magnesium silicate.\|The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. The present invention accordingly provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|This invention relates to a process for the mineralization of carbon dioxide from, for example, a gas stream such as the flue gases from an industrial combustion process.\|	(EP2718230)\|MAGNESIUM 2 CARBONATE(100,20)\|MAGNESIUM 2 CARBONATE COMPOUND(100,9)\|METHANEDIONE MINERALIZATION(100,5)\|METHANEDIONE CAPTURE(33,1)\|MAGNESIUM SILICATE(29,79)\|METHANEDIONE(26,25)\|MAGNESIUM SILICATE ROCK(22,6)\|ALKALI METAL CARBONATE(19,60)\|MAJOR TECHNICAL DIFFICULTY(19,1)\|OUTGOING HOT GAS(19,1)\|PRECONCENTRATION(19,1)\|MOVING GRATE FURNACE(18,2)\|SPECIALIZED EQUIPMENT(18,1)\|ALKALI METAL(17,115)\|ALKALI METAL BICARBONATE(17,10)\|OUTGOING HOT SOLID(17,1)\|ALKALI METAL MAGNESIUM SILICATE(16,33)\|GAS PURIFICATION(16,1)\|FURNACE(14,4)\|MAGNESIUM SILICATE MINERAL(14,3)\|INCOMING SOLID(14,1)\|PRESSURIZING(14,1)\|METHANEDIONE GAS(13,4)\|FINELY GROUND MAGNESIUM SILICATE(13,1)\|MOLAR RATIO(12,6)\|CARBONATION(12,2)\|MOVING GRATE(11,5)\|INCOMING COMBUSTION AIR(11,1)\|COUNTERCURRENT HEAT EXCHANGE(10,3)\|NET ENERGY CONSUMPTION(10,2)\|COOLED DECARBONATED PELLET(9,4)\|PELLET(8,14)\|SIO(8,5)\|GAS STREAM(8,3)\|CO2(7,18)\|MGO(7,13)\|PRESSURE ELEVATION(7,3)\|COMBUSTION(7,2)\|FLUE GAS(6,7)\|GAS SCRUBBING(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|PREHEATER CYCLONE TOWER(6,1)\|HYDROMAGNESITE(5,10)\|ALKALI METAL HYDROXIDE(5,3)\|LAB FURNACE(5,3)\|EARTH CRUST(5,2)\|LASER GRANULOMETRY(5,2)\|PLATINUM CRUCIBLE(5,2)\|UNREACTED OLIVINE(5,2)\|ASBESTOS FIBRILLAR(5,1)\|DECARBONATED NODULE(5,1)\|OBSCURATION STABILIZATION(5,1)\|MG2SIO(4,6)\|FORSTERITE(4,5)\|AMORPHOUS PRODUCT(4,4)\|ENERGY EFFICIENCY(4,3)\|ANHYDROUS MAGNESIUM SILICATE(4,2)\|DECARBONATION REACTION(4,2)\|EXCESS METHANEDIONE(4,2)\|PRESSURE REACTOR(4,2)\|ABSORB METHANEDIONE(4,1)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|GASEOUS METHANEDIONE(4,1)\|HEAT TRANSFER(4,1)\|HELICOIDAL TEFLON(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|PREHEATER TOWER(4,1)\|REACTION PRODUCT(3,7)\|ATMOSPHERIC PRESSURE(3,5)\|PARTICULATE(3,5)\|FILTER CAKE DRYING(3,3)\|FUEL COMBUSTION GAS(3,3)\|NITRITE(3,3)\|BURNING ZONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|GASEOUS CO2(3,2)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GROUND OLIVINE MIX(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SUSPENSION PREHEATER(3,1)\|TALC IDDINGSITE(3,1)\|ALKALI METAL OXIDE(2,6)\|AQUEOUS SOLUTION(2,4)\|EXPERIMENT(2,4)\|HOT GAS(2,4)\|R2CO(2,4)\|ROTARY KILN(2,4)\|AQUEOUS SUSPENSION(2,3)\|MGCO(2,3)\|STOICHIOMETRIC RATIO(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANHYDROUS PRODUCT(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|MEASURED LOI DATA(2,2)\|MIXED POWDER(2,2)\|PYROXENE(2,2)\|SIEVING(2,2)\|SODIUM CARBONATE POWDER(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|ALKALINE FLUX(2,1)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CO2 GRAM(2,1)\|COMBINED CO2 QUANTITATIVE DETECTION(2,1)\|CRUSHED SAMPLE(2,1)\|DISSOLVED BICARBONATE SALT(2,1)\|EARTH MANTLE COMPONENT(2,1)\|ESTIMATED MG(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE NESS(2,1)\|FINE SAND GRANULOMETRY(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|MAXIMUM CO2 CAPTURE(2,1)\|MAXIMUM SLURRY ADDITIVE(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|NONTOXIC WASTE(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|PELLET R2O SILICA RATIO(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|QUALITATIVE PHASE(2,1)\|R2O MOLAR RATIO(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SILICATE HYDROXIDE(2,1)\|SKIN CLEANING(2,1)\|SLURRY CONC(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|STEEL CRUCIBLE(2,1)\|SULFUR CONTENT(2,1)\|SUSPENSION AGITATION(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|ADSORPTION(1,1)\|AMORPHOUS SOLID RICH(1,1)\|ANALYZING IMAGE(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BICARBONATE SOLUTION(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CAO SILICA MOLAR RATIO(1,1)\|CARBONATE PRODUCT(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|CONVERSION YIELD(1,1)\|COUNTERCURRENT(1,1)\|CRYSTALLINE PHASE(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FEO SILICA MOLAR RATIO(1,1)\|FILTER CAKE MG(1,1)\|FILTERCAKE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GLASS REACTOR(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT WATER CIRCULATION(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|HYPERSTHENE(1,1)\|INCOMING AIR(1,1)\|LIQUID FILTRATE(1,1)\|LITHIUM MAGNESIUM SODIUM SILICATE(1,1)\|\|(EP2718230)\|MAGNESIUM 2 CARBONATE(100,20)\|MAGNESIUM 2 CARBONATE COMPOUND(100,9)\|METHANEDIONE MINERALIZATION(100,5)\|METHANEDIONE CAPTURE(33,1)\|MAGNESIUM SILICATE(29,79)\|METHANEDIONE(26,25)\|MAGNESIUM SILICATE ROCK(22,6)\|ALKALI METAL CARBONATE(19,60)\|MAJOR TECHNICAL DIFFICULTY(19,1)\|OUTGOING HOT GAS(19,1)\|PRECONCENTRATION(19,1)\|MOVING GRATE FURNACE(18,2)\|SPECIALIZED EQUIPMENT(18,1)\|ALKALI METAL(17,115)\|ALKALI METAL BICARBONATE(17,10)\|OUTGOING HOT SOLID(17,1)\|ALKALI METAL MAGNESIUM SILICATE(16,33)\|GAS PURIFICATION(16,1)\|FURNACE(14,4)\|MAGNESIUM SILICATE MINERAL(14,3)\|INCOMING SOLID(14,1)\|PRESSURIZING(14,1)\|METHANEDIONE GAS(13,4)\|FINELY GROUND MAGNESIUM SILICATE(13,1)\|MOLAR RATIO(12,6)\|CARBONATION(12,2)\|MOVING GRATE(11,5)\|INCOMING COMBUSTION AIR(11,1)\|COUNTERCURRENT HEAT EXCHANGE(10,3)\|NET ENERGY CONSUMPTION(10,2)\|COOLED DECARBONATED PELLET(9,4)\|PELLET(8,14)\|SIO(8,5)\|GAS STREAM(8,3)\|CO2(7,18)\|MGO(7,13)\|PRESSURE ELEVATION(7,3)\|COMBUSTION(7,2)\|FLUE GAS(6,7)\|GAS SCRUBBING(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|PREHEATER CYCLONE TOWER(6,1)\|HYDROMAGNESITE(5,10)\|ALKALI METAL HYDROXIDE(5,3)\|LAB FURNACE(5,3)\|EARTH CRUST(5,2)\|LASER GRANULOMETRY(5,2)\|PLATINUM CRUCIBLE(5,2)\|UNREACTED OLIVINE(5,2)\|ASBESTOS FIBRILLAR(5,1)\|DECARBONATED NODULE(5,1)\|OBSCURATION STABILIZATION(5,1)\|MG2SIO(4,6)\|FORSTERITE(4,5)\|AMORPHOUS PRODUCT(4,4)\|ENERGY EFFICIENCY(4,3)\|ANHYDROUS MAGNESIUM SILICATE(4,2)\|DECARBONATION REACTION(4,2)\|EXCESS METHANEDIONE(4,2)\|PRESSURE REACTOR(4,2)\|ABSORB METHANEDIONE(4,1)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|GASEOUS METHANEDIONE(4,1)\|HEAT TRANSFER(4,1)\|HELICOIDAL TEFLON(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|PREHEATER TOWER(4,1)\|REACTION PRODUCT(3,7)\|ATMOSPHERIC PRESSURE(3,5)\|PARTICULATE(3,5)\|FILTER CAKE DRYING(3,3)\|FUEL COMBUSTION GAS(3,3)\|NITRITE(3,3)\|BURNING ZONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|GASEOUS CO2(3,2)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GROUND OLIVINE MIX(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SUSPENSION PREHEATER(3,1)\|TALC IDDINGSITE(3,1)\|ALKALI METAL OXIDE(2,6)\|AQUEOUS SOLUTION(2,4)\|EXPERIMENT(2,4)\|HOT GAS(2,4)\|R2CO(2,4)\|ROTARY KILN(2,4)\|AQUEOUS SUSPENSION(2,3)\|MGCO(2,3)\|STOICHIOMETRIC RATIO(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANHYDROUS PRODUCT(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|MEASURED LOI DATA(2,2)\|MIXED POWDER(2,2)\|PYROXENE(2,2)\|SIEVING(2,2)\|SODIUM CARBONATE POWDER(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|ALKALINE FLUX(2,1)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CO2 GRAM(2,1)\|COMBINED CO2 QUANTITATIVE DETECTION(2,1)\|CRUSHED SAMPLE(2,1)\|DISSOLVED BICARBONATE SALT(2,1)\|EARTH MANTLE COMPONENT(2,1)\|ESTIMATED MG(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE NESS(2,1)\|FINE SAND GRANULOMETRY(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|MAXIMUM CO2 CAPTURE(2,1)\|MAXIMUM SLURRY ADDITIVE(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|NONTOXIC WASTE(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|PELLET R2O SILICA RATIO(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|QUALITATIVE PHASE(2,1)\|R2O MOLAR RATIO(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SILICATE HYDROXIDE(2,1)\|SKIN CLEANING(2,1)\|SLURRY CONC(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|STEEL CRUCIBLE(2,1)\|SULFUR CONTENT(2,1)\|SUSPENSION AGITATION(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|ADSORPTION(1,1)\|AMORPHOUS SOLID RICH(1,1)\|ANALYZING IMAGE(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BICARBONATE SOLUTION(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CAO SILICA MOLAR RATIO(1,1)\|CARBONATE PRODUCT(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|CONVERSION YIELD(1,1)\|COUNTERCURRENT(1,1)\|CRYSTALLINE PHASE(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FEO SILICA MOLAR RATIO(1,1)\|FILTER CAKE MG(1,1)\|FILTERCAKE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GLASS REACTOR(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT WATER CIRCULATION(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|HYPERSTHENE(1,1)\|INCOMING AIR(1,1)\|LIQUID FILTRATE(1,1)\|LITHIUM MAGNESIUM SODIUM SILICATE(1,1)\|\|(EP2532624)\|MAGNESIUM 2 CARBONATE(100,22)\|MAGNESIUM 2 CARBONATE COMPOUND(100,11)\|METHANEDIONE MINERALIZATION(100,6)\|METHANEDIONE CAPTURE(30,1)\|MAGNESIUM SILICATE(28,78)\|METHANEDIONE(27,22)\|MAGNESIUM SILICATE ROCK(20,6)\|ALKALI METAL CARBONATE(18,59)\|PRECONCENTRATION(18,1)\|ALKALI METAL MAGNESIUM SILICATE(17,34)\|MAJOR TECHNICAL DIFFICULTY(17,1)\|OUTGOING HOT GAS(17,1)\|ALKALI METAL(16,115)\|ALKALI METAL BICARBONATE(16,10)\|MOVING GRATE FURNACE(16,2)\|SPECIALIZED EQUIPMENT(16,1)\|OUTGOING HOT SOLID(15,1)\|GAS PURIFICATION(14,1)\|FURNACE(13,4)\|MAGNESIUM SILICATE MINERAL(13,3)\|INCOMING SOLID(13,1)\|PRESSURIZING(13,1)\|METHANEDIONE GAS(12,4)\|FINELY GROUND MAGNESIUM SILICATE(12,1)\|MOLAR RATIO(11,6)\|BICARBONATE(11,5)\|CARBONATION(11,2)\|MOVING GRATE(10,5)\|NET ENERGY CONSUMPTION(10,2)\|INCOMING COMBUSTION AIR(10,1)\|COUNTERCURRENT HEAT EXCHANGE(9,3)\|PRESSURE ELEVATION(9,1)\|PELLET(8,14)\|COOLED DECARBONATED PELLET(8,4)\|GAS STREAM(8,3)\|MGO(7,8)\|SIO(7,6)\|CO2(6,16)\|FLUE GAS(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|COMBUSTION(6,2)\|ALKALI METAL SILICATE(6,1)\|PREHEATER CYCLONE TOWER(6,1)\|GAS SCRUBBING(5,7)\|UNREACTED OLIVINE(5,2)\|MG2SIO(4,7)\|ALKALI METAL HYDROXIDE(4,3)\|EARTH CRUST(4,2)\|LASER GRANULOMETRY(4,2)\|PLATINUM CRUCIBLE(4,2)\|ASBESTOS FIBRILLAR(4,1)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|DECARBONATED NODULE(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|OBSCURATION STABILIZATION(4,1)\|FORSTERITE(3,5)\|HYDROMAGNESITE(3,5)\|ATMOSPHERIC PRESSURE(3,4)\|PARTICULATE(3,4)\|ENERGY EFFICIENCY(3,3)\|R2MGSIO(3,3)\|ANHYDROUS MAGNESIUM SILICATE(3,2)\|BURNING ZONE(3,2)\|EXCESS METHANEDIONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|GASEOUS CO2(3,2)\|LAB FURNACE(3,2)\|PRESSURE REACTOR(3,2)\|ABSORB METHANEDIONE(3,1)\|CO2 HINGE(3,1)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GASEOUS METHANEDIONE(3,1)\|GROUND OLIVINE MIX(3,1)\|HEAT TRANSFER(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|PREHEATER TOWER(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SUSPENSION PREHEATER(3,1)\|ALKALI METAL OXIDE(2,6)\|REACTION PRODUCT(2,5)\|AQUEOUS SOLUTION(2,4)\|HOT GAS(2,4)\|R2CO(2,4)\|ROTARY KILN(2,4)\|FUEL COMBUSTION GAS(2,3)\|NITRITE(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|FILTERCAKE(2,2)\|MEASURED LOI DATA(2,2)\|PYROXENE(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CO2 GRAM(2,1)\|DECARBONATION REACTION(2,1)\|EARTH MANTLE COMPONENT(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE PRECIPITATE(2,1)\|FINE SAND GRANULOMETRY(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|MAXIMUM CO2 CAPTURE(2,1)\|MAXIMUM SLURRY ADDITIVE(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MICROCRYSTALLINE SILICA PRODUCT(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|PELLET R2O SILICA RATIO(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|R2O MOLAR RATIO(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SLURRY CONC(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|SULFUR CONTENT(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|MGCO(1,3)\|STOICHIOMETRIC RATIO(1,3)\|EXPERIMENT(1,2)\|ANALYZING IMAGE(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CAO SILICA MOLAR RATIO(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|COUNTERCURRENT(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FEO SILICA MOLAR RATIO(1,1)\|FILTRATE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|HYPERSTHENE(1,1)\|IDDINGSITE(1,1)\|INCOMING AIR(1,1)\|LIZARDITE(1,1)\|\|(US9469546)\|MAGNESIUM 2 CARBONATE(100,21)\|MAGNESIUM 2 CARBONATE COMPOUND(100,10)\|METHANEDIONE MINERALIZATION(100,6)\|MAGNESIUM SILICATE(39,77)\|MOLAR RATIO(32,8)\|METHANEDIONE(30,22)\|ALKALI METAL CARBONATE(29,58)\|COMPOSITION R2O(26,1)\|MAJOR TECHNICAL DIFFICULTY(25,1)\|OUTGOING HOT GAS(25,1)\|ALKALI METAL(24,112)\|MOVING GRATE FURNACE(24,2)\|SPECIALIZED EQUIPMENT(24,1)\|OUTGOING HOT SOLID(23,1)\|ALKALI METAL MAGNESIUM SILICATE(21,32)\|GAS PURIFICATION(21,1)\|ALKALI METAL BICARBONATE(19,9)\|MAGNESIUM SILICATE ROCK(19,6)\|FURNACE(19,4)\|MAGNESIUM SILICATE MINERAL(19,3)\|INCOMING SOLID(19,1)\|PRESSURIZING(19,1)\|METHANEDIONE GAS(18,4)\|FINELY GROUND MAGNESIUM SILICATE(17,1)\|CARBONATION(16,2)\|MOVING GRATE(15,5)\|INCOMING COMBUSTION AIR(15,1)\|COUNTERCURRENT HEAT EXCHANGE(14,3)\|NET ENERGY CONSUMPTION(14,2)\|COOLED DECARBONATED PELLET(12,4)\|PELLET(11,14)\|MGO(11,11)\|SIO(11,5)\|MINERAL(10,8)\|SLURRY(9,10)\|BED(9,5)\|PRESSURE ELEVATION(9,3)\|GAS SCRUBBING(8,7)\|HEAT EXCHANGE(8,4)\|PREHEATER CYCLONE TOWER(8,1)\|UNREACTED OLIVINE(7,2)\|ASBESTOS FIBRILLAR(7,1)\|DECARBONATED NODULE(7,1)\|OBSCURATION STABILIZATION(7,1)\|MG2SIO(6,7)\|AMORPHOUS PRODUCT(6,4)\|ALKALI METAL HYDROXIDE(6,3)\|LAB FURNACE(6,3)\|EARTH CRUST(6,2)\|LASER GRANULOMETRY(6,2)\|PLATINUM CRUCIBLE(6,2)\|CO2 MAXIMIZING CAPTURE(6,1)\|COUNTER CURRENT HEAT EXCHANGE(6,1)\|METHANEDIONE CAPTURE(6,1)\|METHANEDIONE GAS LIBERATION(6,1)\|HYDROMAGNESITE(5,6)\|FORSTERITE(5,5)\|PARTICULATE(5,5)\|ENERGY EFFICIENCY(5,3)\|ANHYDROUS MAGNESIUM SILICATE(5,2)\|BURNING ZONE(5,2)\|DECARBONATION REACTION(5,2)\|EXCESS METHANEDIONE(5,2)\|GASEOUS CO2(5,2)\|PRESSURE REACTOR(5,2)\|SLURRY ADDITIVE(5,2)\|ABSORB METHANEDIONE(5,1)\|CO2 SLURRY(5,1)\|GASEOUS METHANEDIONE(5,1)\|HEAT TRANSFER(5,1)\|HELICOIDAL TEFLON(5,1)\|PREHEATER TOWER(5,1)\|REACTION PRODUCT(4,7)\|ALKALI METAL OXIDE(4,6)\|FUEL COMBUSTION GAS(4,3)\|NITRITE(4,3)\|GAS ABSORBER COLUMN(4,2)\|COMPOSITION OLIVINE SAND(4,1)\|CRYSTALIZATION SPECIALIZATION(4,1)\|GROUND OLIVINE MIX(4,1)\|LASER GRANULOMETER(4,1)\|MAGNESIUM SILICATE CARBONATION(4,1)\|MAXIMIZATION(4,1)\|MAXIMIZE CAPTURE(4,1)\|SAMPLE DEAGGLOMERATION(4,1)\|SLURRY TEMP(4,1)\|SUSPENSION PREHEATER(4,1)\|R2CO(3,5)\|AQUEOUS SOLUTION(3,4)\|HOT GAS(3,4)\|ROTARY KILN(3,4)\|ACTINOLITE(3,2)\|AMOSITE(3,2)\|AMPHIBOLE(3,2)\|ANTHOPHYLLITE(3,2)\|CHLORITE(3,2)\|CHRYSOTILE(3,2)\|ENSTATITE(3,2)\|MEASURED LOI DATA(3,2)\|MIXED POWDER(3,2)\|PYROXENE(3,2)\|R2MGSIO(3,2)\|SIEVING(3,2)\|SULFITE(3,2)\|TREMOLITE(3,2)\|ULTRASOUND(3,2)\|ANHYDROUS DURATION PRODUCT(3,1)\|BASIC MAGNESIUM ORTHOSILICATE(3,1)\|BIOMASS DERIVED FUEL(3,1)\|BLUE DIODE(3,1)\|CALCULATION MATRIX(3,1)\|CARBONATABLE SOLID(3,1)\|CO2 GRAM(3,1)\|COMBINED CO2 QUANTITATIVE DETECTION(3,1)\|CRUSHED SAMPLE(3,1)\|EARTH MANTLE COMPONENT(3,1)\|ESTIMATED MG(3,1)\|EXPERIMENT CAPTURED VOLUME(3,1)\|FERMENTATION RESIDUE GAS(3,1)\|FINE NESS(3,1)\|FINE SAND GRANULOMETRY(3,1)\|GAS SCRUBBER(3,1)\|HOT NODULE HEAT(3,1)\|INCOMING COMBUSTION AIR PREHEATER(3,1)\|INORGANIC IMPURITY(3,1)\|MAXIMUM CO2 CAPTURE(3,1)\|METHANEDIONE GAS ACTION(3,1)\|MINERALIZATION(3,1)\|MOVING GRATE COOLER(3,1)\|NATURALLY OCCURRING MINERAL(3,1)\|OLIVINE SAMPLE(3,1)\|OUTGOING SOLID PARTICLE(3,1)\|PACKED BED COLUMN(3,1)\|PELLET R2O SILICA RATIO(3,1)\|POROUS BED(3,1)\|POWDER SELF NODULIZE(3,1)\|PRECONCENTRATION(3,1)\|PREHEATER TOP CYCLONE(3,1)\|QUALITATIVE PHASE(3,1)\|R2O MOLAR RATIO(3,1)\|REACTED SAMPLE PHASE CONSTITUTION(3,1)\|REACTION ESCAPE(3,1)\|RED HE NE LASER(3,1)\|SAMPLE REACTION(3,1)\|SCRUBBING FLUE GAS(3,1)\|SESQUIHYDRATE(3,1)\|SILICA MOLE(3,1)\|SOLID PRECIPITATION(3,1)\|SOLUBLE SALT(3,1)\|STABLE NODULE(3,1)\|STEEL CRUCIBLE(3,1)\|SULFUR CONTENT(3,1)\|SUSPENSION AGITATION(3,1)\|UNREACTED MAGNESIUM SILICATE(3,1)\|WORKING SESSION(3,1)\|AQUEOUS SUSPENSION(2,3)\|STOICHIOMETRIC RATIO(2,3)\|GAS STREAM(2,2)\|ADSORPTION(2,1)\|ANALYZING IMAGE(2,1)\|ANHYDROUS PRODUCT(2,1)\|ANHYDROUS SODIUM CARBONATE(2,1)\|ANTIGORITE(2,1)\|AQUEOUS ACID(2,1)\|AUTOCLAVE(2,1)\|BASIC MAGNESIUM SILICATE(2,1)\|BRONZITE(2,1)\|BURNER(2,1)\|CALCINATION(2,1)\|CAO SILICA MOLAR RATIO(2,1)\|CARBONATE PRODUCT(2,1)\|CHONDRODITE(2,1)\|CLOSED REACTOR(2,1)\|COMPLEX MAGNESIUM(2,1)\|CONVERSION YIELD(2,1)\|COUNTERCURRENT(2,1)\|DECAHYDRATE(2,1)\|DECARBONATION DEGREE(2,1)\|DECOMPOSITION(2,1)\|DIHYDRATE(2,1)\|DIOPSIDE(2,1)\|EXPRESSED REACTION(2,1)\|FAYALITE(2,1)\|FE2SIO(2,1)\|FEO SILICA MOLAR RATIO(2,1)\|FILTER CAKE DRYING(2,1)\|FILTERCAKE(2,1)\|FINE POWDER(2,1)\|GARNIERITE(2,1)\|GLASS REACTOR(2,1)\|GRANULE(2,1)\|HECTORITE(2,1)\|HOT WATER CIRCULATION(2,1)\|HOT ZONE(2,1)\|HUMITE(2,1)\|HYPERSTHENE(2,1)\|IDDINGSITE(2,1)\|INCOMING AIR(2,1)\|LIQUID FILTRATE(2,1)\|LIZARDITE(2,1)\|\|(US20140120022)\|MAGNESIUM 2 CARBONATE(100,22)\|MAGNESIUM 2 CARBONATE COMPOUND(100,11)\|METHANEDIONE MINERALIZATION(100,6)\|MAGNESIUM SILICATE(31,82)\|METHANEDIONE CAPTURE(31,1)\|METHANEDIONE(27,23)\|MAGNESIUM SILICATE ROCK(21,6)\|ALKALI METAL CARBONATE(19,60)\|ALKALI METAL(18,119)\|ALKALI METAL MAGNESIUM SILICATE(18,37)\|COMPOSITION R2O(18,1)\|MAJOR TECHNICAL DIFFICULTY(18,1)\|OUTGOING HOT GAS(18,1)\|PRECONCENTRATION(18,1)\|MOVING GRATE FURNACE(17,2)\|SPECIALIZED EQUIPMENT(17,1)\|ALKALI METAL BICARBONATE(16,10)\|FORMULA SI SILICA(16,1)\|OUTGOING HOT SOLID(16,1)\|GAS PURIFICATION(15,1)\|PRESSURIZING(14,1)\|FURNACE(13,4)\|MAGNESIUM SILICATE MINERAL(13,3)\|INCOMING SOLID(13,1)\|METHANEDIONE GAS(12,4)\|FINELY GROUND MAGNESIUM SILICATE(12,1)\|MOLAR RATIO(11,6)\|CARBONATION(11,2)\|MOVING GRATE(10,5)\|COUNTERCURRENT HEAT EXCHANGE(10,3)\|NET ENERGY CONSUMPTION(10,2)\|INCOMING COMBUSTION AIR(10,1)\|COOLED DECARBONATED PELLET(9,4)\|PELLET(8,14)\|GAS STREAM(8,3)\|CO2(7,19)\|MGO(7,12)\|COMBUSTION(7,2)\|FLUE GAS(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|SIO(6,4)\|PRESSURE ELEVATION(6,3)\|PREHEATER CYCLONE TOWER(6,1)\|GAS SCRUBBING(5,7)\|UNREACTED OLIVINE(5,2)\|ASBESTOS FIBRILLAR(5,1)\|DECARBONATED NODULE(5,1)\|OBSCURATION STABILIZATION(5,1)\|HYDROMAGNESITE(4,6)\|MG2SIO(4,6)\|FORSTERITE(4,5)\|AMORPHOUS PRODUCT(4,4)\|ALKALI METAL HYDROXIDE(4,3)\|LAB FURNACE(4,3)\|EARTH CRUST(4,2)\|LASER GRANULOMETRY(4,2)\|PLATINUM CRUCIBLE(4,2)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|ATMOSPHERIC PRESSURE(3,5)\|PARTICULATE(3,5)\|ENERGY EFFICIENCY(3,3)\|ANHYDROUS MAGNESIUM SILICATE(3,2)\|BURNING ZONE(3,2)\|DECARBONATION REACTION(3,2)\|EXCESS METHANEDIONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|GASEOUS CO2(3,2)\|PRESSURE REACTOR(3,2)\|SLURRY ADDITIVE(3,2)\|ABSORB METHANEDIONE(3,1)\|CO2 SLURRY(3,1)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GASEOUS METHANEDIONE(3,1)\|GROUND OLIVINE MIX(3,1)\|HEAT TRANSFER(3,1)\|HELICOIDAL TEFLON(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|PREHEATER TOWER(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SLURRY TEMP(3,1)\|SUSPENSION PREHEATER(3,1)\|REACTION PRODUCT(2,7)\|ALKALI METAL OXIDE(2,6)\|AQUEOUS SOLUTION(2,4)\|HOT GAS(2,4)\|R2CO(2,4)\|ROTARY KILN(2,4)\|FUEL COMBUSTION GAS(2,3)\|NITRITE(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|MEASURED LOI DATA(2,2)\|MIXED POWDER(2,2)\|PYROXENE(2,2)\|SIEVING(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|ANHYDROUS DURATION PRODUCT(2,1)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CO2 GRAM(2,1)\|COMBINED CO2 QUANTITATIVE DETECTION(2,1)\|CRUSHED SAMPLE(2,1)\|EARTH MANTLE COMPONENT(2,1)\|ESTIMATED MG(2,1)\|EXPERIMENT CAPTURED VOLUME(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE NESS(2,1)\|FINE SAND GRANULOMETRY(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|MAXIMUM CO2 CAPTURE(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|PELLET R2O SILICA RATIO(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|QUALITATIVE PHASE(2,1)\|R2O MOLAR RATIO(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|STEEL CRUCIBLE(2,1)\|SULFUR CONTENT(2,1)\|SUSPENSION AGITATION(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|AQUEOUS SUSPENSION(1,3)\|STOICHIOMETRIC RATIO(1,3)\|ADSORPTION(1,1)\|AMORPHOUS SOLID RICH(1,1)\|ANALYZING IMAGE(1,1)\|ANHYDROUS PRODUCT(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CAO SILICA MOLAR RATIO(1,1)\|CARBONATE PRODUCT(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|CONVERSION YIELD(1,1)\|COUNTERCURRENT(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|EXPRESSED REACTION(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FEO SILICA MOLAR RATIO(1,1)\|FILTER CAKE DRYING(1,1)\|FILTERCAKE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GLASS REACTOR(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT WATER CIRCULATION(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|HYPERSTHENE(1,1)\|IDDINGSITE(1,1)\|INCOMING AIR(1,1)\|\|(WO2012/168176)\|MAGNESIUM 2 CARBONATE(100,18)\|MAGNESIUM 2 CARBONATE COMPOUND(100,9)\|METHANEDIONE MINERALIZATION(100,5)\|METHANEDIONE CAPTURE(49,1)\|MAGNESIUM SILICATE(47,81)\|METHANEDIONE(39,22)\|MAGNESIUM SILICATE ROCK(32,6)\|FORMULA SI(30,2)\|ALKALI METAL CARBONATE(29,59)\|MAJOR TECHNICAL DIFFICULTY(28,1)\|OUTGOING HOT GAS(28,1)\|PRECONCENTRATION(28,1)\|ALKALI METAL(27,117)\|ALKALI METAL MAGNESIUM SILICATE(27,36)\|MOVING GRATE FURNACE(27,2)\|SPECIALIZED EQUIPMENT(27,1)\|ALKALI METAL BICARBONATE(26,10)\|FORMULA SI SILICA(25,1)\|OUTGOING HOT SOLID(25,1)\|GAS PURIFICATION(23,1)\|FURNACE(21,4)\|MAGNESIUM SILICATE MINERAL(21,3)\|INCOMING SOLID(21,1)\|PRESSURIZING(21,1)\|METHANEDIONE GAS(20,4)\|FINELY GROUND MAGNESIUM SILICATE(19,1)\|CARBONATION(17,2)\|MOLAR RATIO(16,9)\|MOVING GRATE(16,5)\|NET ENERGY CONSUMPTION(16,2)\|INCOMING COMBUSTION AIR(16,1)\|COUNTERCURRENT HEAT EXCHANGE(15,3)\|COOLED DECARBONATED PELLET(14,4)\|GAS STREAM(13,3)\|PELLET(12,14)\|MGO(11,10)\|COMBUSTION(11,2)\|BED(10,5)\|PRESSURE ELEVATION(10,3)\|FLUE GAS(9,7)\|GAS SCRUBBING(9,7)\|HEAT EXCHANGE(9,4)\|PREHEATER CYCLONE TOWER(9,1)\|LARGELY AMORPHOUS PRODUCT CERAMICS(8,4)\|UNREACTED OLIVINE(8,2)\|ALKALI METAL HYDROXIDE(7,3)\|LAB FURNACE(7,3)\|EARTH CRUST(7,2)\|LASER GRANULOMETRY(7,2)\|PLATINUM CRUCIBLE(7,2)\|ASBESTOS FIBRILLAR(7,1)\|COUNTER CURRENT HEAT EXCHANGE(7,1)\|DECARBONATED NODULE(7,1)\|METHANEDIONE GAS LIBERATION(7,1)\|OBSCURATION STABILIZATION(7,1)\|FORSTERITE(6,5)\|ENERGY EFFICIENCY(6,3)\|ANHYDROUS MAGNESIUM SILICATE(6,2)\|DECARBONATION REACTION(6,2)\|EXCESS METHANEDIONE(6,2)\|PRESSURE REACTOR(6,2)\|SLURRY ADDITIVE(6,2)\|ABSORB METHANEDIONE(6,1)\|GASEOUS METHANEDIONE(6,1)\|HEAT TRANSFER(6,1)\|HELICOIDAL TEFLON(6,1)\|PREHEATER TOWER(6,1)\|ATMOSPHERIC PRESSURE(5,5)\|PARTICULATE(5,5)\|BURNING ZONE(5,2)\|COMPOSITION OLIVINE SAND(5,1)\|CRYSTALIZATION SPECIALIZATION(5,1)\|LASER GRANULOMETER(5,1)\|MAGNESIUM SILICATE CARBONATION(5,1)\|MAXIMIZE CAPTURE(5,1)\|SAMPLE DEAGGLOMERATION(5,1)\|SUSPENSION PREHEATER(5,1)\|MG2SI(4,7)\|REACTION PRODUCT(4,7)\|FUEL COMBUSTION GAS(4,3)\|HYDROMAGNESITE(4,3)\|NITRITE(4,3)\|R2MGSI(4,3)\|GAS ABSORBER COLUMN(4,2)\|EARTH MANTLE COMPONENT(4,1)\|FERMENTATION RESIDUE GAS(4,1)\|FINE NESS(4,1)\|FINE SAND GRANULOMETRY(4,1)\|INORGANIC IMPURITY(4,1)\|LN EXPERIMENT(4,1)\|MOVING GRATE COOLER(4,1)\|OLIVINE SAMPLE(4,1)\|PACKED BED COLUMN(4,1)\|QUANTITATIVE DETECTION(4,1)\|STABLE NODULE(4,1)\|SUSPENSION AGITATION(4,1)\|UNREACTED MAGNESIUM SILICATE(4,1)\|WORKING SESSION(4,1)\|ALKALI METAL OXIDE(3,6)\|R2C(3,5)\|AQUEOUS SOLUTION(3,4)\|HOT GAS(3,4)\|MGC(3,4)\|ROTARY KILN(3,4)\|AQUEOUS SUSPENSION(3,3)\|STOICHIOMETRIC RATIO(3,3)\|ACTINOLITE(3,2)\|AMOSITE(3,2)\|AMPHIBOLE(3,2)\|ANTHOPHYLLITE(3,2)\|CHLORITE(3,2)\|CHRYSOTILE(3,2)\|ENSTATITE(3,2)\|MEASURED LOI DATA(3,2)\|MIXED POWDER(3,2)\|PYROXENE(3,2)\|SIEVING(3,2)\|SULFITE(3,2)\|TREMOLITE(3,2)\|ULTRASOUND(3,2)\|BASIC MAGNESIUM ORTHOSILICATE(3,1)\|BIOMASS DERIVED FUEL(3,1)\|BLUE DIODE(3,1)\|CALCULATION MATRIX(3,1)\|CARBONATABLE SOLID(3,1)\|CRUSHED SAMPLE(3,1)\|GAS SCRUBBER(3,1)\|HOT NODULE HEAT(3,1)\|INCOMING COMBUSTION AIR PREHEATER(3,1)\|METHANEDIONE GAS ACTION(3,1)\|MINERALIZATION(3,1)\|NATURALLY OCCURRING MINERAL(3,1)\|OUTGOING SOLID PARTICLE(3,1)\|POROUS BED(3,1)\|POWDER SELF NODULIZE(3,1)\|PREHEATER TOP CYCLONE(3,1)\|QUALITATIVE PHASE(3,1)\|REACTED SAMPLE PHASE CONSTITUTION(3,1)\|REACTION ESCAPE(3,1)\|RED HE NE LASER(3,1)\|SAMPLE REACTION(3,1)\|SCRUBBING FLUE GAS(3,1)\|SESQUIHYDRATE(3,1)\|SILICA MOLE(3,1)\|SOLID PRECIPITATION(3,1)\|SOLUBLE SALT(3,1)\|STEEL CRUCIBLE(3,1)\|SULFUR CONTENT(3,1)\|ADSORPTION(2,1)\|AMORPHOUS SOLID CERAMICS(2,1)\|ANALYZING IMAGE(2,1)\|ANHYDROUS SODIUM CARBONATE(2,1)\|ANTIGORITE(2,1)\|AQUEOUS ACID(2,1)\|AUTOCLAVE(2,1)\|BASIC MAGNESIUM SILICATE(2,1)\|BRONZITE(2,1)\|BURNER(2,1)\|CALCINATION(2,1)\|CARBONATE PRODUCT(2,1)\|CHONDRODITE(2,1)\|CLOSED REACTOR(2,1)\|COMPLEX MAGNESIUM(2,1)\|CONVERSION YIELD(2,1)\|COUNTERCURRENT(2,1)\|DECAHYDRATE(2,1)\|DECARBONATION DEGREE(2,1)\|DECOMPOSITION(2,1)\|DIHYDRATE(2,1)\|DIOPSIDE(2,1)\|FAYALITE(2,1)\|FE2SI(2,1)\|FILTER CAKE DRYING(2,1)\|FILTERCAKE(2,1)\|FINE POWDER(2,1)\|GARNIERITE(2,1)\|GLASS REACTOR(2,1)\|GRANULE(2,1)\|HECTORITE(2,1)\|HOT WATER CIRCULATION(2,1)\|HOT ZONE(2,1)\|HUMITE(2,1)\|HYPERSTHENE(2,1)\|IDDINGSITE(2,1)\|INCOMING AIR(2,1)\|\|(CN103582611)\|MAGNESIUM 2 CARBONATE(100,17)\|MAGNESIUM 2 CARBONATE COMPOUND(100,9)\|MINERALIZING METHANEDIONE(100,2)\|MINERALIZE METHANEDIONE(100,1)\|FORMULA R2AN(37,1)\|FORMULA SIO2THE REACTION(37,1)\|METHANEDIONE(34,20)\|MAGNESIUM SILICATE(31,67)\|ALKALI MAGNESIUM SILICATE(28,25)\|ALKALI METAL CARBONATE(27,55)\|ALKALI METAL MAGNESIUM SILICATE(22,4)\|ALKALI METAL(21,76)\|ALKALI METAL BICARBONATE(19,8)\|BICARBONATE(18,6)\|MOLAR RATIO(13,6)\|PARTICULATE(10,6)\|COOLED DECARBONATED PELLET(9,2)\|GAS SCRUBBING(8,7)\|MAGNESIUM SILICATE ROCK(8,4)\|OLIVINE SAND(8,3)\|XH2O(8,2)\|LABORATORY FURNACE PLATINUM CRUCIBLE(8,1)\|METHANEDIONE MINERALIZATION(8,1)\|ALKALI METAL HYDROXIDE(7,3)\|DECARBONATED NODULE(7,1)\|LASER GRANULOMETRY(6,2)\|2SIO4OF GROUND OLIVINESAND(6,1)\|MAGNESIUM SILICATE1AMORPHOUS PRODUCT CARBONATION(6,1)\|MGCO SEPARATELY3AND(6,1)\|PERILLYL PYROXENE(6,1)\|PREHEATER CYCLONE COLUMN(6,1)\|UNREACTED OLIVESSTONE(6,1)\|SILICA RICH(5,3)\|DECARBONATION REACTION(5,2)\|EXCESS METHANEDIONE(5,2)\|SLURRY ADDITIVE(5,2)\|ABSORB METHANEDIONE(5,1)\|GASEOUS METHANEDIONE(5,1)\|OLIVINE STONE(5,1)\|PERCOLATED CAKE(5,1)\|PREHEATER TOWER(5,1)\|RELEASING METHANEDIONE(5,1)\|UNREACTED OLIVINE(5,1)\|ASBESTOS(4,4)\|CHRYSOTILE(4,3)\|NITRITE(4,3)\|COMBUSTION ZONE(4,2)\|GAS ABSORBER COLUMN(4,2)\|MAGNESIUM SILICATE MINERAL(4,2)\|ADDED2TO RETURN(4,1)\|ANHYDROUS MAGNESIUM SILICATE(4,1)\|CALCIUM FORSTERITE(4,1)\|FERMENTATION RESIDUE GAS(4,1)\|GASEOUS CO2UP(4,1)\|INORGANIC IMPURITY(4,1)\|LASER GRANULOMETER(4,1)\|MAGNESIUM REACTION(4,1)\|MAXIMUM THEORETICAL VALUE2AND(4,1)\|METHANEDIONE MIXING(4,1)\|METHANEDIONE VOLUME(4,1)\|MOVING GRATE COOLER(4,1)\|MOVING GRATE FURNACE(4,1)\|OLIVINE SAMPLE(4,1)\|PELLET BED(4,1)\|POROUS FRIT(4,1)\|PRECIPITATED SOLID PLUS SOLIDS1IN(4,1)\|ROCK ELEMENTAL ANALYSIS(4,1)\|SAMPLE DEAGGLOMERATION(4,1)\|SILICA MOLE(4,1)\|SLURRY ABSORPTION(4,1)\|STABLE NODULE(4,1)\|SUSPENSION PREHEATER(4,1)\|TRAVELING GRATE SPEED(4,1)\|UNREACTED MAGNESIUM SILICATE(4,1)\|AQUEOUS SOLUTION(3,4)\|ROTARY KILN(3,4)\|EXPERIMENT(3,3)\|STIRRER(3,3)\|ACTINOLITE(3,2)\|AMPHIBOLE(3,2)\|CHLORITE(3,2)\|ENSTATITE(3,2)\|FUEL COMBUSTION GAS(3,2)\|GAS STREAM(3,2)\|LOI DATA(3,2)\|MIXED POWDER(3,2)\|NET ENERGY CONSUMPTION(3,2)\|SIEVING(3,2)\|SODIUM CARBONATE HYDRATE POWDER(3,2)\|SODIUM CARBONATE POWDER(3,2)\|SODIUM CARBONATE SAMPLE(3,2)\|SULFITE(3,2)\|TREMOLITE(3,2)\|ULTRASOUND(3,2)\|ABOVETHE(3,1)\|ATMOSPHERE ABSOLUTE(3,1)\|BASIC MAGNESIUM ORTHOSILICATE(3,1)\|BIOMASS DERIVED FUEL(3,1)\|BLUE DIODE(3,1)\|BOUND ANALYSIS(3,1)\|CALCULATION MATRIX(3,1)\|CARBON DIOXIDERELEASING GAS(3,1)\|CO2CONTINUOUSLY(3,1)\|CRUSHED SAMPLE(3,1)\|EARTH CRUST DEEP LAYER(3,1)\|EFFLUENT GAS(3,1)\|GAS SCRUBBER(3,1)\|INCOMING COMBUSTION AIR PREHEATER(3,1)\|MAGNESIUM SILICATE HYDROXIDE(3,1)\|MANTLE2SIO COMPONENT(3,1)\|METHANEDIONE GAS ACTION(3,1)\|METHANEDIONE LEVEL(3,1)\|MGO SIO2THE MOLAR RATIO(3,1)\|NATURALLY OCCURRING MINERAL(3,1)\|OUTGOING HOT GAS(3,1)\|OUTGOING SOLID PARTICLE(3,1)\|PACKED BED(3,1)\|PASSINGTHE REACTION PRODUCT(3,1)\|POROUS BED(3,1)\|PREHEATER TOP CYCLONE(3,1)\|PREHEATER WALL(3,1)\|PROCESSES2AND(3,1)\|PROCESSES2THE EXHAUST GAS(3,1)\|QUANTITATIVE DETECTION(3,1)\|RED HE NE LASER(3,1)\|SAMPLE REACTION(3,1)\|SCRUBBING FLUE GAS(3,1)\|STEEL CRUCIBLE(3,1)\|STIRRED SUSPENSION(3,1)\|SULFUR CONTENT(3,1)\|ALKALI METAL OXIDE(2,5)\|AQUEOUS SUSPENSION(2,3)\|2CO3MOLAR(2,1)\|2SIO4MOLAR(2,1)\|AGITATION(2,1)\|AGITATOR SPEED(2,1)\|ALKALI METAL CARBONATESONE MOLE(2,1)\|ANHYDROUS SODIUM CARBONATE(2,1)\|ANTIGORITE(2,1)\|AUTOCLAVE(2,1)\|BRONZITE(2,1)\|BURNER(2,1)\|CALCINATION(2,1)\|CARBONATE RATIO(2,1)\|CARCINOGEN(2,1)\|CLOSED REACTOR(2,1)\|CO2THE LATTER VERTICAL ARROW(2,1)\|COMPLEX MAGNESIUM(2,1)\|DECAHYDRATE(2,1)\|DECARBONATION DEGREE(2,1)\|DECOMPOSITION(2,1)\|DIBUTONITE(2,1)\|DIHYDRATE(2,1)\|DIOPSIDE(2,1)\|DRY POWDER(2,1)\|ENERGY INTENSIVE(2,1)\|FAYALITE(2,1)\|FIBRIL(2,1)\|GAS2AND WATER(2,1)\|GLASS REACTOR(2,1)\|GRAM2CONSUMING(2,1)\|GROUND MAGNESIUM SILICATE(2,1)\|HEATING2SIO(2,1)\|HECTORITE(2,1)\|HELICOID(2,1)\|HOT WATER CIRCULATION(2,1)\|HOT ZONE(2,1)\|INCOMING SOLID(2,1)\|LEAVING ROOM(2,1)\|LIQUID FILTRATE(2,1)\|\|(CN103582611)\|MAGNESIUM 2 CARBONATE(100,19)\|MAGNESIUM 2 CARBONATE COMPOUND(100,11)\|MINERALIZE METHANEDIONE(100,3)\|MINERALIZING METHANEDIONE(61,2)\|MAGNESIUM SILICATE(35,81)\|METHANEDIONE(35,23)\|ALKALI MAGNESIUM SILICATE(31,30)\|MAGNESIUM SILICATE ROCK(23,6)\|ALKALI METAL CARBONATE(22,61)\|MAGNESIUM SILICATE COMPOUND(22,3)\|HEATED MIXTURE2O(22,1)\|PRECONCENTRATION(21,1)\|MAJOR TECHNICAL DIFFICULTY(20,1)\|SPECIALIZED EQUIPMENT(19,1)\|ALKALI METAL(18,87)\|ALKALI METAL BICARBONATE(18,10)\|MOVING GRATE(18,5)\|CARBONATION RATE(17,1)\|ELECTRICITY(17,1)\|FORMULA SIO2THE REACTION(17,1)\|GAS PURIFICATION(17,1)\|FORMULA R2AN(16,1)\|MAGNESIUM SILICATE MINERAL(15,3)\|ALKALI METAL MAGNESIUM SILICATE(14,4)\|MOLAR RATIO(12,7)\|BICARBONATE(12,6)\|CARBONATE SOURCE(12,1)\|SILICATE(11,3)\|GRANULE(10,1)\|PRESSURIZING(10,1)\|PELLET(9,15)\|COUNTERCURRENT HEAT EXCHANGE(9,4)\|SIO(9,4)\|GAS STREAM(9,3)\|MGO(8,8)\|PARTICULATE(8,6)\|FURNACE(8,4)\|COMBUSTION(8,2)\|BED(7,5)\|OLIVINE SAND(7,4)\|PRESSURE ELEVATION(7,3)\|COOLED DECARBONATED PELLET(7,2)\|FLUE GAS(6,7)\|GAS SCRUBBING(6,7)\|ATMOSPHERIC PRESSURE(6,5)\|STOICHIOMETRIC RATIO(6,3)\|UNREACTED OLIVINE(6,2)\|XH2O(6,2)\|LABORATORY FURNACE PLATINUM CRUCIBLE(6,1)\|METHANEDIONE MINERALIZATION(6,1)\|ALKALI METAL HYDROXIDE(5,3)\|LASER PARTICLE SIZER(5,2)\|DECARBONATED NODULE(5,1)\|MAGNESIUM SILICATE1AMORPHOUS PRODUCT CARBONATION(5,1)\|MGCO SEPARATELY3AND(5,1)\|PERILLYL PYROXENE(5,1)\|PREHEATER CYCLONE COLUMN(5,1)\|ENERGY EFFICIENCY(4,3)\|SILICA RICH(4,3)\|DECARBONATION REACTION(4,2)\|EXCESS METHANEDIONE(4,2)\|HEAT EXCHANGE(4,2)\|SLURRY ADDITIVE(4,2)\|ABSORB METHANEDIONE(4,1)\|GASEOUS METHANEDIONE(4,1)\|HEAT TRANSFER(4,1)\|OLIVINE STONE(4,1)\|PERCOLATED CAKE(4,1)\|PREHEATER TOWER(4,1)\|RELEASING METHANEDIONE(4,1)\|REACTION PRODUCT(3,8)\|ASBESTOS(3,4)\|CHRYSOTILE(3,3)\|NITRITE(3,3)\|COMBUSTION ZONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|ADDED2TO RETURN(3,1)\|ANHYDROUS MAGNESIUM SILICATE(3,1)\|AQUEOUS SLURRY(3,1)\|CALCIUM FORSTERITE(3,1)\|FERMENTATION RESIDUE GAS(3,1)\|GASEOUS CO2UP(3,1)\|INORGANIC IMPURITY(3,1)\|LASER GRANULOMETRY(3,1)\|MAGNESIUM REACTION(3,1)\|MAXIMUM THEORETICAL VALUE2AND(3,1)\|METAL OXIDE(3,1)\|METHANEDIONE GAS RELEASE(3,1)\|METHANEDIONE MIXING(3,1)\|METHANEDIONE VOLUME(3,1)\|MOVING GRATE COOLER(3,1)\|MOVING GRATE FURNACE(3,1)\|OLIVINE SAMPLE(3,1)\|PELLET BED(3,1)\|POROUS FRIT(3,1)\|PRECIPITATED SOLID PLUS SOLIDS1IN(3,1)\|PREHEAT KILN INCOMING COMBUSTION AIR(3,1)\|ROCK ELEMENTAL ANALYSIS(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SILICA MOLE(3,1)\|SLURRY ABSORPTION(3,1)\|STABLE NODULE(3,1)\|SUSPENSION PREHEATER(3,1)\|TRAVELING GRATE SPEED(3,1)\|UNREACTED MAGNESIUM SILICATE(3,1)\|CARBON DIOXIDE(2,14)\|AQUEOUS SOLUTION(2,4)\|ROTARY KILN(2,4)\|AQUEOUS SUSPENSION(2,3)\|EXPERIMENT(2,3)\|STIRRER(2,3)\|ACTINOLITE(2,2)\|AMPHIBOLE(2,2)\|ENSTATITE(2,2)\|FUEL COMBUSTION GAS(2,2)\|LOI DATA(2,2)\|MIXED POWDER(2,2)\|NET ENERGY CONSUMPTION(2,2)\|SIEVING(2,2)\|SODIUM CARBONATE HYDRATE POWDER(2,2)\|SODIUM CARBONATE POWDER(2,2)\|SODIUM CARBONATE SAMPLE(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|ATMOSPHERE ABSOLUTE(2,1)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|BOUND ANALYSIS(2,1)\|CALCULATION MATRIX(2,1)\|CO2CONTINUOUSLY(2,1)\|CRUSHED SAMPLE(2,1)\|EARTH CRUSTCHLORITE DEEP LAYER(2,1)\|EFFLUENT GAS(2,1)\|GAS SCRUBBER(2,1)\|MAGNESIUM SILICATE HYDROXIDE(2,1)\|MANTLE2SIO COMPONENT(2,1)\|METHANEDIONE GAS ACTION(2,1)\|METHANEDIONE LEVEL(2,1)\|MGO SIO2THE MOLAR RATIO(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|OUTGOING HOT GAS(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED(2,1)\|POROUS BED(2,1)\|PREHEATER TOP CYCLONE(2,1)\|PREHEATER WALL(2,1)\|PROCESSES2AND(2,1)\|PROCESSES2THE EXHAUST GAS(2,1)\|QUANTITATIVE DETECTION(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|STIRRED SUSPENSION(2,1)\|SULFUR CONTENT(2,1)\|2CO3MOLAR(1,1)\|2SIO4MOLAR(1,1)\|2SIO4THE(1,1)\|AGITATION(1,1)\|AGITATOR SPEED(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AUTOCLAVE(1,1)\|BASETHE(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CARBONATE RATIO(1,1)\|CARCINOGEN(1,1)\|CLOSED REACTOR(1,1)\|CO2THE LATTER VERTICAL ARROW(1,1)\|COMPLEX MAGNESIUM(1,1)\|COMPOUNDS2O(1,1)\|COUNTERCURRENT(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIBUTONITE(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|DRY POWDER(1,1)\|ENERGY INTENSIVE(1,1)\|FAYALITE(1,1)\|FIBRIL(1,1)\|FINENESS(1,1)\|GAS2AND WATER(1,1)\|GLASS REACTOR(1,1)\|GRAM2CONSUMING(1,1)\|\|(KR10-2014-0045459)\|MAGNESIUM CARBONATE(100,19)\|MAGNESIUM CARBONATE COMPOUND(100,11)\|MINERALIZING CARBON DIOXIDE(100,2)\|ASBESTOS MICROFIBER(95,1)\|PROPORTION CARBONATION(86,1)\|MINERALIZE CARBON DIOXIDE(73,4)\|MICROPOLISHED MAGNESIUM SILICATE(70,1)\|MAGNESIUM SILICATE(68,80)\|ROCK MAGNESIUM SILICATE(56,1)\|PRECONCENTRATION(51,1)\|ALKALI METAL BICARBONATE(50,15)\|HOT EFFLUENT GAS(47,1)\|ALKALI METAL CARBONATE(45,64)\|GAS PURIFICATION(45,1)\|TECHNICAL DIFFICULTY(45,1)\|HOT EFFLUENT SOLID(42,1)\|ALKALI METAL(40,124)\|ALKALI METAL MAGNESIUM SILICATE(40,35)\|MAGNESIUM SILICATE ROCK(40,4)\|HYDRATING WATER(40,1)\|PRESSURIZING(39,1)\|MAGNESIUM SILICATE MINERAL(36,4)\|INCOMING SOLID(34,1)\|COMBUSTION(33,2)\|CARBON DIOXIDE(32,34)\|ANHYDROUS ALKALI METAL CARBONATE(32,1)\|BICARBONATE(30,7)\|MAGNESIUM SILICATE REACTION(30,5)\|MOLE(29,40)\|INCOMING COMBUSTION AIR(29,1)\|ALKALI METAL SILICATE(28,1)\|COUNTERCURRENT HEAT EXCHANGE(26,3)\|NET ENERGY CONSUMPTION(26,2)\|HEALTH(26,1)\|FURNACE(25,4)\|ANHYDROUS ALKALI METAL(25,1)\|GAS STREAM(23,3)\|EARTH OLIVINE(19,4)\|PRESSURE ELEVATION(19,3)\|MOLAR RATIO(18,4)\|ENERGY CONSUMPTION(18,1)\|FLUE GAS(17,7)\|PREHEATER CYCLONE TOWER(17,1)\|CARBON DIOXIDE GAS(16,4)\|ABRADED OLIVINE SAND(15,1)\|MAGNESIUM SILICATE CARBONATION(15,1)\|ALKALI METAL HYDROXIDE(13,3)\|EXPERIMENTAL FURNACE(13,3)\|PREDOMINANTLY AMORPHOUS PRODUCT(13,3)\|EARTH MANTLE(13,2)\|EARTH PERCEPTION(13,2)\|PLATINUM CRUCIBLE(13,2)\|CLEANING GAS(12,7)\|SILICON DIOXIDE(12,4)\|COOLED DECARBONATED PALLET(12,1)\|DECARBONATED CLUMP(12,1)\|GALLATE SOPHILITE(12,1)\|MITIGATION WHEEHMITE(12,1)\|PALLET PACKED BED(12,1)\|DISRUPTION(11,6)\|PARTICULATE(11,6)\|ANHYDROUS MAGNESIUM SILICATE(11,2)\|DECARBONATION REACTION(11,2)\|MOVING GRATE FURNACE(11,2)\|PRESSURE REACTOR(11,2)\|HEAT EXCHANGE(10,3)\|HELICOIDAL TEFLON(10,1)\|KAOLIN OLIVINE(10,1)\|PREHEATER TOWER(10,1)\|UNREACTED OLIVINE(10,1)\|ATMOSPHERIC PRESSURE(9,5)\|CRYSTALIZATION SPECIALIZATION(9,1)\|LASER GRANULOMETER(9,1)\|LASER GRANULOMETRY(9,1)\|MAX CO2(9,1)\|PALLET BATCH(9,1)\|PALLET BED(9,1)\|SAMPLE DEAGGLOMERATION(9,1)\|SHIELD STABILIZATION(9,1)\|SUSPENSION PREHEATER(9,1)\|REACTION PRODUCT(8,8)\|ATINITE(8,3)\|FUEL COMBUSTION GAS(8,3)\|HYDROMAGNESITE(8,3)\|NITRITE(8,3)\|COMBUSTION ZONE(8,2)\|GAS ABSORBER COLUMN(8,2)\|AQUEOUS SOLUTION(7,4)\|ADHEREND FORMATION(7,1)\|BEEN CONSIDERED CARCINOGEN(7,1)\|CO2 ATM(7,1)\|COMPUTATIONAL MATRIX(7,1)\|FERMENTATION RESIDUE GAS(7,1)\|INDUSTRIAL APPLICATION(7,1)\|INORGANIC IMPURITY(7,1)\|IRON OLIVINE(7,1)\|MAGNESIUM SILICATE HYDRATE(7,1)\|OLIVINE SAMPLE(7,1)\|PACKED BED COLUMN(7,1)\|SLURRY ADDITIVE(7,1)\|STABLE NODULE(7,1)\|UNREACTED MAGNESIUM SILICATE(7,1)\|WARM WOOL(7,1)\|HOT GAS(6,4)\|ROTARY KILN(6,4)\|MG2SI(6,3)\|ACTINOLITE(6,2)\|CHLORITE(6,2)\|INTERRUPTION(6,2)\|MEASURED LOI DATA(6,2)\|MIXED POWDER(6,2)\|SIEVING(6,2)\|SODIUM CARBONATE HYDRATE POWDER(6,2)\|SODIUM CARBONATE SAMPLE(6,2)\|SULFITE(6,2)\|ULTRASOUND(6,2)\|ALWAYS PURE SILICATE(6,1)\|BASIC MAGNESIUM NONANOATE(6,1)\|BLUE DIODE(6,1)\|DRIED FILTER DEBRIS(6,1)\|EFFLUENT GAS(6,1)\|EFFLUENT SOLID PARTICLE(6,1)\|EXAMPLE2SI(6,1)\|FE2SI04PAUL(6,1)\|GAS SCRUBBER(6,1)\|GAS SCRUBBING(6,1)\|HEATING JACKET(6,1)\|HOT NODULE HEAT(6,1)\|INCOMING COMBUSTION AIR PREHEATER(6,1)\|JOINED FILTRATE(6,1)\|KILN OUTLET GAS(6,1)\|MINERALIZATION(6,1)\|PALLET MECHANICAL INTEGRITY(6,1)\|PALLETIZATION(6,1)\|POLYDISPERSITY(6,1)\|POROUS BED(6,1)\|POTASSIUM CARBONATE HYDRATE(6,1)\|PREHEATER TOP CYCLONE(6,1)\|QUALITATIVE PHASE(6,1)\|RED HE NE LASER(6,1)\|SAMPLE MEASURED IGNITION(6,1)\|SAMPLE REACTION(6,1)\|SILICINICKELITE(6,1)\|SOLID PRECIPITATION(6,1)\|SOLUBLE SALT(6,1)\|STEEL CRUCIBLE(6,1)\|STOICHIOMETRY RATIO(6,1)\|SUBPREFERRED STOICHIOMETRIC RATIO(6,1)\|SULFUR CONTENT(6,1)\|AQUEOUS SUSPENSION(5,3)\|MAJOR SOLID PRODUCT(5,3)\|MGCO3(5,3)\|UNITY(5,3)\|PELLET(5,2)\|ABSORB CARBON DIOXIDE(4,1)\|ACID DILUTION(4,1)\|ADDRESSING(4,1)\|ADSORPTION(4,1)\|ANHYDRIDE(4,1)\|ANHYDROUS SODIUM CARBONATE(4,1)\|ANTHOPHYLLITE(4,1)\|ASBESTOS(4,1)\|AUTOCLAVE(4,1)\|BASIC MAGNESIUM SILICATE(4,1)\|BIOMASS(4,1)\|CALCINATION(4,1)\|CARBON DIOXIDE CONVERSION(4,1)\|CARBONATE RATIO(4,1)\|CASE2SI(4,1)\|CHONDRODITE(4,1)\|CLEANING FLUE GAS(4,1)\|CLOSED REACTOR(4,1)\|COMBINED CO2(4,1)\|COMBUSTOR(4,1)\|COUNTERCURRENT(4,1)\|DECAHYDRATE(4,1)\|DECARBONATION DEGREE(4,1)\|DECOMPOSITION(4,1)\|DEEP LAYER(4,1)\|DISINTEGRATION(4,1)\|DRY POWDER(4,1)\|ENERGY INTENSIVE(4,1)\|FINAL MELT(4,1)\|FINAL POWDER(4,1)\|FINE POWDER(4,1)\|GALLSTONE(4,1)\|GASEOUS CARBON DIOXIDE(4,1)\|GLASS REACTOR(4,1)\|GRATING(4,1)\|HECTORITE(4,1)\|HEMIHYDRATE(4,1)\|HEURITE(4,1)\|HOT WATER CIRCULATION(4,1)\|HOT ZONE(4,1)\|HYDRATION WATER(4,1)\|IDINSITE(4,1)\|INCLUSIVE SHAPE(4,1)\|\|(CA2838035)\|MAGNESIUM 2 CARBONATE(100,20)\|MAGNESIUM 2 CARBONATE COMPOUND(100,11)\|METHANEDIONE MINERALIZATION(100,6)\|METHANEDIONE CAPTURE(30,1)\|MAGNESIUM SILICATE(27,82)\|METHANEDIONE(27,23)\|MAGNESIUM SILICATE ROCK(20,6)\|PRECONCENTRATION(18,1)\|ALKALI METAL MAGNESIUM SILICATE(17,37)\|MAJOR TECHNICAL DIFFICULTY(17,1)\|OUTGOING HOT GAS(17,1)\|ALKALI METAL CARBONATE(16,60)\|MOVING GRATE FURNACE(16,2)\|SPECIALIZED EQUIPMENT(16,1)\|OUTGOING HOT SOLID(15,1)\|ALKALI METAL(14,119)\|GAS PURIFICATION(14,1)\|GROUND MAGNESIUM SILICATE(14,1)\|ALKALI METAL BICARBONATE(13,10)\|FURNACE(13,4)\|MAGNESIUM SILICATE MINERAL(13,3)\|INCOMING SOLID(13,1)\|PRESSURIZING(13,1)\|METHANEDIONE GAS(12,4)\|BICARBONATE(11,5)\|CARBONATION(11,2)\|MOVING GRATE(10,5)\|NET ENERGY CONSUMPTION(10,2)\|INCOMING COMBUSTION AIR(10,1)\|COUNTERCURRENT HEAT EXCHANGE(9,3)\|PELLET(8,14)\|COOLED DECARBONATED PELLET(8,4)\|GAS STREAM(8,3)\|XH2O(7,1)\|MOLAR RATIO(6,9)\|FLUE GAS(6,7)\|BED(6,5)\|HEAT EXCHANGE(6,4)\|PRESSURE ELEVATION(6,3)\|COMBUSTION(6,2)\|PREHEATER CYCLONE TOWER(6,1)\|GAS SCRUBBING(5,7)\|UNREACTED OLIVINE(5,2)\|HYDROMAGNESITE(4,6)\|AMORPHOUS PRODUCT(4,4)\|ALKALI METAL HYDROXIDE(4,3)\|LAB FURNACE(4,3)\|EARTH CRUST(4,2)\|LASER GRANULOMETRY(4,2)\|PLATINUM CRUCIBLE(4,2)\|ASBESTOS FIBRILLAR(4,1)\|COUNTER CURRENT HEAT EXCHANGE(4,1)\|DECARBONATED NODULE(4,1)\|METHANEDIONE GAS LIBERATION(4,1)\|OBSCURATION STABILIZATION(4,1)\|ATMOSPHERIC PRESSURE(3,5)\|FORSTERITE(3,5)\|PARTICULATE(3,5)\|FILTER CAKE DRYING(3,4)\|ANHYDROUS PRODUCT(3,3)\|ENERGY EFFICIENCY(3,3)\|ANHYDROUS MAGNESIUM SILICATE(3,2)\|BURNING ZONE(3,2)\|DECARBONATION REACTION(3,2)\|EXCESS METHANEDIONE(3,2)\|GAS ABSORBER COLUMN(3,2)\|PRESSURE REACTOR(3,2)\|SLURRY ADDITIVE(3,2)\|ABSORB METHANEDIONE(3,1)\|COMPOSITION OLIVINE SAND(3,1)\|CRYSTALIZATION SPECIALIZATION(3,1)\|GASEOUS METHANEDIONE(3,1)\|GROUND OLIVINE MIX(3,1)\|HEAT TRANSFER(3,1)\|HELICOIDAL TEFLON(3,1)\|HYDRO MAGNESITE(3,1)\|LASER GRANULOMETER(3,1)\|MAGNESIUM SILICATE CARBONATION(3,1)\|MAXIMIZE CAPTURE(3,1)\|PREHEATER TOWER(3,1)\|SAMPLE DEAGGLOMERATION(3,1)\|SUSPENSION PREHEATER(3,1)\|REACTION PRODUCT(2,7)\|EXPERIMENT(2,5)\|AQUEOUS SOLUTION(2,4)\|HOT GAS(2,4)\|ROTARY KILN(2,4)\|FUEL COMBUSTION GAS(2,3)\|MG2SIO(2,3)\|NITRITE(2,3)\|ACTINOLITE(2,2)\|AMOSITE(2,2)\|AMPHIBOLE(2,2)\|ANTHOPHYLLITE(2,2)\|CHLORITE(2,2)\|CHRYSOTILE(2,2)\|ENSTATITE(2,2)\|MEASURED LOI DATA(2,2)\|MG094FE(2,2)\|MGO SI(2,2)\|MIXED POWDER(2,2)\|PYROXENE(2,2)\|SIEVING(2,2)\|SODIUM CARBONATE POWDER(2,2)\|SULFITE(2,2)\|TREMOLITE(2,2)\|ULTRASOUND(2,2)\|BASIC MAGNESIUM ORTHOSILICATE(2,1)\|BIOMASS DERIVED FUEL(2,1)\|BLUE DIODE(2,1)\|CALCULATION MATRIX(2,1)\|CARBONATABLE SOLID(2,1)\|CRUSHED SAMPLE(2,1)\|EARTH MANTLE COMPONENT(2,1)\|ESTIMATED MG(2,1)\|FERMENTATION RESIDUE GAS(2,1)\|FINE NESS(2,1)\|FINE SAND GRANULOMETRY(2,1)\|FORMULA SI(2,1)\|GAS SCRUBBER(2,1)\|HOT NODULE HEAT(2,1)\|INCOMING COMBUSTION AIR PREHEATER(2,1)\|INORGANIC IMPURITY(2,1)\|METHANEDIONE GAS ACTION(2,1)\|MINERALIZATION(2,1)\|MOVING GRATE COOLER(2,1)\|NATURALLY OCCURRING MINERAL(2,1)\|OLIVINE SAMPLE(2,1)\|OUTGOING SOLID PARTICLE(2,1)\|PACKED BED COLUMN(2,1)\|POROUS BED(2,1)\|POWDER SELF NODULIZE(2,1)\|PREHEATER TOP CYCLONE(2,1)\|QUALITATIVE PHASE(2,1)\|QUANTITATIVE DETECTION(2,1)\|REACTED SAMPLE PHASE CONSTITUTION(2,1)\|REACTION ESCAPE(2,1)\|RED HE NE LASER(2,1)\|SAMPLE REACTION(2,1)\|SCRUBBING FLUE GAS(2,1)\|SELFNODULIZATION(2,1)\|SESQUIHYDRATE(2,1)\|SILICA MOLE(2,1)\|SOLID PRECIPITATION(2,1)\|SOLUBLE SALT(2,1)\|STABLE NODULE(2,1)\|STEEL CRUCIBLE(2,1)\|SULFUR CONTENT(2,1)\|SUSPENSION AGITATION(2,1)\|UNREACTED MAGNESIUM SILICATE(2,1)\|WORKING SESSION(2,1)\|AQUEOUS SUSPENSION(1,3)\|CO2(1,3)\|STOICHIOMETRIC RATIO(1,3)\|ADSORPTION(1,1)\|AMORPHOUS SOLID RICH(1,1)\|ANALYZING IMAGE(1,1)\|ANHYDROUS SODIUM CARBONATE(1,1)\|ANTIGORITE(1,1)\|AQUEOUS ACID(1,1)\|AUTOCLAVE(1,1)\|BASIC MAGNESIUM SILICATE(1,1)\|BRONZITE(1,1)\|BURNER(1,1)\|CALCINATION(1,1)\|CARBONATE PRODUCT(1,1)\|CHONDRODITE(1,1)\|CLOSED REACTOR(1,1)\|COMPLEX MAGNESIUM(1,1)\|CONVERSION YIELD(1,1)\|COUNTERCURRENT(1,1)\|CRYSTALLINE PHASE(1,1)\|DECAHYDRATE(1,1)\|DECARBONATION DEGREE(1,1)\|DECOMPOSITION(1,1)\|DIHYDRATE(1,1)\|DIOPSIDE(1,1)\|ENERGY INTENSIVE(1,1)\|FAYALITE(1,1)\|FE2SIO(1,1)\|FILTERCAKE(1,1)\|FINE POWDER(1,1)\|GARNIERITE(1,1)\|GLASS REACTOR(1,1)\|GRANULE(1,1)\|HECTORITE(1,1)\|HOT WATER CIRCULATION(1,1)\|HOT ZONE(1,1)\|HUMITE(1,1)\|	(EP2718230)\|1. A process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|2. A process according to claim 1 in which the carbon dioxide is in the free form in a gas comprising carbon dioxide.\|3. A process according to claim 1 in which the carbon dioxide is in the form of an alkali metal carbonate or bicarbonate formed by contacting a gas comprising carbon dioxide with an alkali metal hydroxide or an alkali metal carbonate.\|4. A process according to any one of the preceding claims in which the alkali metal magnesium silicate is prepared by the reaction of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate.\|5. A process according to any one of the preceding claims in which the alkali metal magnesium silicate is prepared by the reaction, at a temperature from 500 to 1100°C, of an alkali metal carbonate compound which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide of the formula SiO2, being from 2:1 to 1:2, which reaction produces an alkali metal magnesium silicate.\|6. A process according to claim 5 in which the reaction is effected at a temperature of 800 to 950°C.\|7. A process according to claim 5 or 6 in which the magnesium silicate is of the general formula m(MgO)-SiO2-xH2O wherein m is from 0.5 to 3 and x is from zero to 2.\|8. A process according to any one of claims 5 to 7 in which the reaction of the alkali metal carbonate compound and the magnesium silicate is effected in the solid state.\|9. A process according to any one of the preceding claims in which the alkali metal magnesium silicate is in shaped or particulate form.	(EP2718230)\|[0001] This invention relates to a process for the mineralization of carbon dioxide from, for example, a gas stream such as the flue gases from an industrial combustion process. The process uses as starting material an alkali metal magnesium silicate and produces magnesium carbonate compounds and silica.\|[0002] In WO 2010/097451 magnesium-comprising silicate hydroxide particles are heated alone to activate the particles, which are then ground to a smaller size and contacted with an aqueous medium (which preferably contains a dissolved bicarbonate salt) and carbon dioxide under low temperature conditions. The solution and small activated particles are then contacted with carbon dioxide at elevated temperatures (preferably at least 140°C, and therefore under pressure to avoid the water simply boiling off).\|[0003] US2009/0202410 similarly discloses contacting an aqueous alkali metal carbonate solution with carbon dioxide to obtain a bicarbonate solution, which is then contacted with a waste material. The mineral may contain, inter alia, a magnesium-containing silicate mineral.\|[0004] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into magnesium silicate hydrate minerals such as serpentine or chlorite (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10)(OH)2).\|[0005] Magnesium silicate rocks constitute an excellent source of basic magnesium which should in theory readily be converted into stable magnesium carbonate compounds by the action of carbon dioxide gas under normal atmospheric conditions. However, in practice, the weathering and carbonation of natural magnesium silicate minerals at the Earth's surface occurs only very slowly. Thus, while the use of magnesium silicates as a source of basic magnesium for the mineralization of carbon dioxide has been proposed as a means to combat the current trend towards increasing carbon dioxide levels in the atmosphere, processes to achieve such mineralization have heretofore been excessively energy-intensive, as well as excessively expensive to set up and operate, and, and thus have not been commercialized. One of the major technical difficulties which renders such processes so expensive to set up and operate is the need to use elevated pressures and temperatures in order to achieve a sufficiently high rate (for industrial purposes) of carbonation of magnesium silicate minerals. Typically, the carbon dioxide gas must first be purified and then compressed to pressures in excess of 70 atmospheres, and then contacted with finely-ground magnesium silicates in a pressure reactor at temperatures of 120-200°C. This requires specialized equipment which is expensive to build and maintain, as well as large amounts of electric power to operate the gas purification and pressurization process as well as to finely grind the magnesium silicate rocks.\|[0006] Although the common magnesium silicate minerals listed above tend to be very "unreactive," (e.g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a "carbonate fusion", is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analysed by standard chemical techniques, thus allowing for total elemental analysis of the rock. The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0007] US 5,085,838A describes a process for reacting an asbestiform material, which may be a magnesium-containing mineral, with an alkaline flux, which may be an alkali metal carbonate, into an environmentally safe glassy material by heating to about 750°C to 1000°C. An X-ray diffraction spectrum attributes one peak to an alkali metal magnesium silicate. The glassy material produced is described as a safe, non-toxic waste, which can be disposed of, or used as a process feed-stock for producing various glassy products.\|[0008] JP2007/146094 describes the use of a water-swelling clay, named as sodium-magnesium silicate, in a detergent composition suitable for cleaning skin. The clay, which is a known material, is not a true alkali metal magnesium silicate, contains lithium as part of its structure and is known by a number of synonyms including lithium magnesium sodium salt, synthetic magnesium lithium silicate and lithium magnesium sodium silicate.\|[0009] The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step.\|[0010] The present invention accordingly provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|[0011] The alkali metal is preferably potassium or, more preferably, sodium.\|[0012] The process is preferably effected at a temperature of 25 to 100°C, more preferably 35 to 80°C. The carbon dioxide may be in the free form in a gas comprising carbon dioxide.\|[0013] The process of the invention can be used to remove carbon dioxide from a gas at a reduced or elevated pressure or, for example, at about atmospheric pressure. The process of the invention may be carried out on a carbon dioxide-containing gas at an absolute pressure generally from 0.5 to 100 bar, preferably from 1 to 20 bar, most preferably at about 1 bar.\|[0014] The gas to be treated may contain from 0.01% to 100% carbon dioxide by volume, preferably from 0.1% to 50%, more preferably from 1% to 40%, and most preferably from 4% to 30%. The gas stream may be a flue gas from an industrial combustion process.\|[0015] The carbon dioxide may also be in the form of an alkali metal carbonate or bicarbonate formed by contacting a gas comprising carbon dioxide with an alkali metal hydroxide or an alkali metal carbonate. The alkali metal carbonate or bicarbonate is preferably produced in the form of an aqueous solution, prepared by reaction between an aqueous solution of an alkali metal hydroxide or carbonate and gaseous carbon dioxide.\|[0016] The alkali metal magnesium silicate is preferably in particulate form, for example a powder, preferably having a Blaine specific surface area of 100 to 800m2/kg, more preferably 200 to 650m2/kg.\|[0017] The process according to the invention is preferably effected with a product comprising alkali metal magnesium silicate. The alkali metal magnesium silicate is preferably prepared by the reaction of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate, or a mixture thereof, with a magnesium silicate. The alkali metal carbonate compound used preferably comprises alkali metal carbonate produced by contacting a gas comprising carbon dioxide with an alkali metal magnesium silicate generally in the presence of water, the alkali metal magnesium silicate being converted into a solution of an alkali metal carbonate plus solid residues comprising magnesium carbonates and a largely amorphous product rich in silica and containing some magnesium by reaction with the carbon dioxide, and the alkali metal carbonate solution being separated and concentrated prior to reaction with the magnesium silicate.\|[0018] The invention also provides a process for the preparation of a product comprising an alkali metal magnesium silicate compound (which compound is preferably of composition R2O•MgO•SiO2, (in which R represents an alkali metal),which process comprises the reaction, at a temperature from 500 to 1100°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 2:1 to 1:2, which reaction produces the product comprising an alkali metal magnesium silicate.\|[0019] The product produced by this process may be in shaped or particulate form.\|[0020] The product may be used to provide a slurry, generally aqueous, comprising an alkali metal magnesium silicate produced by this process.\|[0021] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate expressed as silicon dioxide is preferably from 2:1 to 1:2, more preferably from 3:2 to 2:3, for example 4:3 to 3:4. The ratio is most preferably about 1.\|[0022] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used to prepare the alkali metal magnesium silicate.\|[0023] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0024] The magnesium silicate used in the preparation of the alkali metal magnesium silicate is generally a mineral silicate, for example a rock comprising a high concentration, preferably 20% or more, more preferably 50% or more, of a magnesium silicate of the general formula:\| m(MgO)•t(MeO)•SiO2•xH2O\|wherein Me represents a metal or metals other than magnesium, (such as, for example, calcium and/or iron); m is from 0.5 to 3, preferably from1 to 3, t is less than or equal to 1, and x is from zero to 2.\|[0025] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc iddingsite and hectorite. These minerals may contain substantial quantities of calcium, iron and alkali metals in addition to magnesium and silicon. Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, anthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens. The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0026] The mineral silicate used to prepare the alkali metal magnesium silicate is preferably a basic magnesium silicate. The MgO/SiO2 molar ratio is preferably from 1 to 3. The CaO/SiO2 molar ratio is preferably ≤0.5. The FeO/SiO2 molar ratio is preferably ≤0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≤0.2.\|[0027] The alkali metal carbonate compound used in the preparation of the alkali metal magnesium silicate may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2•2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g. chlorides, sulfates, sulfites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates, nitrites or hydroxides) are present which, at the temperature used to prepare the alkali metal magnesium silicate, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0028] The process used to prepare the alkali metal magnesium silicate is preferably effected at a temperature from 600 to 1000°C, for example 700 to 950°C, more preferably from 800 to 950°C. Heating is generally effected for a few minutes to a few hours, for example from 5 minutes to 24 hours, preferably from 10 minutes to 4 hours.\|[0029] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is slightly below its melting point.\|[0030] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as "R2O" in which R represents an alkali metal) present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt. = 140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt. = 106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0031] The magnesium silicate and alkali metal carbonate compound used to prepare the alkali metal magnesium silicate are preferably in particulate form or in shaped form, e.g. as pellets. Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the preparation of the alkali metal magnesium silicate will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of fine sand (grain size 0.06 to 0.2mm) or, if necessary, ground to a fine powder (grain sizes below 0.06mm). Grain sizes greater than 0.06mm are generally determined by sieving. Grain sizes lower than 0.06mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0032] In one embodiment the process to prepare the alkali metal magnesium silicate is conducted in a moving grate furnace.\|[0033] For example a mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in Figure 1 of the accompanying drawings.\|[0034] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0035] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone ("burning zone") just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate:\| (1) Mg2SiO4 + R2CO3 ⇒ product comprising R2MgSiO4 + CO2↑\|in which R is as hereinbefore defined: R preferably represents sodium.\|[0036] The vertical arrow ↑ after CO2 indicates that the carbon dioxide gas produced by this reaction escapes from the bed and exits with the rest of the exhaust gases. The idealized reaction depicted in equation (1) illustrates the production of a product comprising an alkali metal magnesium silicate by direct reaction of a stoichiometric mixture of forsterite and an alkali metal carbonate. This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 2.6 kJ (i.e. about 0.6 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, the net energy consumption for the overall process will be significant. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0037] In a further embodiment, the preparation of the alkali metal magnesium silicate is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln in a decarbonation step which produces carbon dioxide.\|[0038] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0039] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 40% of the total solids volume. In order to achieve this, it may sometimes be necessary to reduce the R2O/SiO2 ratio of the initial pellet composition to a value substantially below the preferred stoichiometric ratio of 1. The degree of reaction of the magnesium silicate during the process will then also be less than 100% but the effect of this can potentially be mitigated by separating the unreacted magnesium silicate from the reaction products and recycling it together with additional magnesium silicate starting material in the production of a fresh batch of pellets.\|[0040] According to a further feature of the invention the preparation of the alkali metal magnesium silicate is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The R2O/SiO2 ratio may be less than 1 if necessary in order to form substantially stable nodules. The nodules are decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0041] The cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate are then used in a gas scrubbing system designed to remove carbon dioxide from a gas at a reduced or elevated pressure or, for example, at about atmospheric pressure.\|[0042] In one embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are ground in water to make an aqueous suspension or slurry which can be directly injected into a conventional gas scrubbing system, such as a spray tower.\|[0043] In another embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are packed into a vertical column to form a packed bed of pellets through which a gas can be passed from bottom to top, while at the same time a suitably-controlled spray of water is added at the top of the column to ensure that the pellets remain wet. This constitutes a counter-current packed-bed gas absorber column. The flow of water leaving the bottom of this column is collected and treated as described later in more detail. The pellets or nodules used to form this type of packed bed column may be pre-selected for their dimensions and mechanical strength.\|[0044] In both of the above embodiments, the reactions occurring in the gas scrubbing system or gas absorber column are as follows:\| (2) R2MgSiO4(S) + (1+p)CO2(g) + water ⇒ (MgO)•p(CO2)•q(H2O)(s) + solid1 + R2CO3 (aq.)\|Where:\| The terms (s), (g) and (aq.) indicate solid, gas, and aqueous solution, respectively,\| p is > 0 and less than or equal to 1. Preferably, p is greater than or equal to 0.5\| q may be zero but can also take values as high as 3 in some cases.\|[0045] The principal solid products are:\| a magnesium carbonate compound, (MgO)•p(CO2)•q(H2O), which may contain more than one chemical compound, and in which a significant fraction of the carbon dioxide captured from the gas stream is contained in a stable solid form; and\| solid1 which is a largely amorphous solid rich in silica and containing some magnesium.\|[0046] These two principal solid products will generally be intimately mixed.\|[0047] Other minor solid products that may also be present include iron oxides, hydroxides or carbonates, as well as calcium carbonates.\|[0048] The alkali metal carbonate solution resulting from the gas scrubbing process will, if reaction (2) goes to completion, contain all of the alkali metal ions present in the original solid product. It is therefore desirable to separate this alkali metal carbonate solution and extract the alkali metal carbonates in solid form for re-use in the high temperature process according to reaction (1). In principle, this can be done most effectively by a combination of evaporation and crystallization processes, making use of the waste heat available both from the decarbonation reaction (1) and also from the flue gas scrubbing system, (noting that reactions (2) and (3) are both highly exothermic and thus that the gas scrubbing system itself is likely to operate at a higher temperature than the temperature of the flue gases being treated by it, thus producing a hot solution of alkali metal carbonate).\|[0049] Some other salts may be present in the alkali metal carbonate solution due to impurities in the magnesium silicate rocks or the flue gases. The most common impurities are likely to be alkali metal sulfates, sulfites, nitrates and nitrites. Under certain circumstances it may be necessary to separate these salts from the recycled alkali metal carbonate by specialized crystallization and washing procedures.\|[0050] In yet another embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are crushed, and if necessary ground, to a suitable median particle size. They are then contacted with a solution comprising an alkali metal bicarbonate in, for example, a tank, preferably with some mechanical stirring. The alkali metal bicarbonate solution may originate from a gas scrubbing system designed to capture carbon dioxide from a gas at, for example, atmospheric pressure. Typical reactions between the alkali-metal bicarbonate solution and the solids in this case is shown by the following equations:\| (3) R2MgSiO4(s) + 2(1+p)RHCO3(aq.) + water ⇒ (MgO)•p(CO2)•q(H2O)(s) + solid1 + (2+p)R2CO3 (aq.)\|[0051] The solid1 is as described above.\|[0052] The alkali metal bicarbonate solution (RHCO3(aq.)) used in reaction (3) may be formed by the reaction of the alkali metal carbonate solution (R2CO3(aq.)) produced in reaction (3) with carbon dioxide and water as shown in reaction (4):\| (4) R2CO3 (aq.) + CO2(g) + water ⇒ 2RHCO3(aq.)\|[0053] This reaction can be conducted in a separate gas scrubbing system, thus participating in a closed-loop alkali-carbonate/bicarbonate gas scrubbing system.\|[0054] The reactions described above are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid magnesium carbonate compounds. The magnesium carbonate solid produced may comprise either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or complex magnesium hydroxy-carbonate hydrates, such as artinite (Mg(OH)2•MgCO3•3H2O), or hydromagnesite, (Mg(OH)2•4MgCO3•4H2O), depending on the conditions. All of these precipitated solids, plus the solid1, will in many cases be finer than the unreacted starting material (Mg2SiO4 in this example), and so could be separated from it by sedimentation and then separated from the alkali metal carbonate which remains in solution by filtration. The unreacted starting material (Mg2SiO4 in this case) thus separated can be recycled to the beginning of the process. The alkali metal carbonate solution can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and also recycled to the start of the process. The mixture of magnesium carbonates and largely amorphous product rich in silica and containing some magnesium produced by these reactions is one of the final products of the overall process (and constitutes a feature of the invention) and can be separated for disposal or for use in other processes.\|[0055] One overall object of the process of the invention is to use common magnesium silicate rocks to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable magnesium carbonate compound.\|[0056] An example of a process of the invention which seeks to maximise capture of CO2 from exhaust gases from other industrial processes and to convert it substantially completely into solid magnesium carbonates in an energy-efficient way, not requiring any high-pressure reactors or autoclaves of the type usually required for direct carbonation of magnesium silicates, is shown in Figure 2 (in which solid1 is a largely amorphous product rich in silica and containing some magnesium).\|[0057] Raw materials are prepared to form a mixture of one part of a magnesium silicate (mMgO.SiO2.xH2O) plus another part being a combination of one or more alkali metal carbonate compounds for which the combined composition is represented by the formula (R2O.nCO2.yH2O); the mixture is heated by fuel combustion gases from a burner supplied with fuel and air; the heated mixture reacts to form a product comprising an alkali metal magnesium silicate (R2O.MgO.SiO2) and to release carbon dioxide which mixes with the fuel combustion gases to form exhaust gases with excess carbon dioxide; liquid water is added to the reaction product and the product is wet ground to form a slurry; the slurry is contacted in a gas scrubber with the exhaust gases with excess carbon dioxide produced earlier and with CO2-containing exhaust gases from other processes to absorb carbon dioxide and to produce a slurry comprising magnesium carbonate and silicon dioxide; the slurry is filtered to produce a filtercake comprising magnesium carbonate and a largely amorphous product rich in silica and containing some magnesium; the filter-cake is dried to produce a mixed solid product which is dried; the filtrate comprising alkali metal carbonate compound in solution is dried or crystallized to produce solid alkali metal carbonate compound which is recycled for use as starting material.\|[0058] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0059] The term "pellets" as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0060] Particle size and size distribution when measured by laser granulometry for particle sizes less than about 100µm are measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He-Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.The apparatus is checked before each working session by means of a standard sample (Sifraco C10 silica) for which the particle size distribution is known.\|[0061] Measurements are performed with the following parameters: pump speed 2300rpm and stirrer speed 800rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30s (for possible air bubbles to clear), a measurement is carried out for 15s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0062] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0063] Particle sizes and particle size distributions for particle sizes greater than about 100µm are measured by sieving.\|[0064] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R, m, t, x, p, n, z and y are as initially defined.\|[0065] The following non-limiting Examples illustrate embodiments of the invention.\|EXAMPLE 1\|[0066] Ground olivine sand of composition (Mg0.94Fe0.06)2SiO4 was mixed with a sodium carbonate hydrate powder in a 14:11 mass ratio. 25g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800°C over 2 hours, maintained at 800°C for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table 1:\|Table 1SampleLoss on IgnitionSodium carbonate powder14.97 %Ground olivine sand0.22 %14:11 mix of ground olivine sand + sodium carbonate powder16.69 %\|[0067] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by X-ray diffraction. The reaction products observed by this technique included Na2MgSiO4 and Fe2O3 together with some unreacted olivine and sodium carbonate.\|EXAMPLE 2\|[0068] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. (The molar ratio of this mixture is close to 1). The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900°C. The sample was air-quenched after 1h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851 °C). The measured loss on ignition of all of the samples is presented in the following Table 2 :\|Table 2SampleLoss on IgnitionSodium carbonate14.96 %Olivine0.04 %Olivine + Sodium carbonate23.02 %\|[0069] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by X-ray diffraction and the main phases detected included Na2MgSiO4, together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data.\|EXAMPLE 3\|[0070] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 litres, maintained at 35°C and agitated with a mechanical stirrer operating at 500rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its adsorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in Table 3.\|Table 3Experiment n°Total CO2 captured (mol)Slurry volume (mL)Slurry conc. (g/L)Total solids, (g)CO2 captured, as % of theoretical maximumSlurry additivesTemp. (°C)Duration (h)Solid products detected10,06412605013,0035Na2CO3: 21,15 g/L3524Hydromagnesite20,07242605013,0040Na2CO3: 53,85 g/L3524Hydromagnesite30,13632605013,0075NaHCO3: 53,85 g/L3530Hydromagnesite40,035226011,52,99843526Artinite\|[0071] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite (Mg(OH)2•4MgCO3•4H2O), and in one case artinite (Mg(OH)2•MgCO3•3H2O), which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 4\|[0072] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometre sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950°C), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio. About 5kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950°C for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by X-ray fluorescence spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3, and 33.4% sodium expressed as Na2O. An X-ray diffraction analysis showed the major phase present in the product to be Na2MgSiO4.\|EXAMPLE 5\|[0073] The reaction products of Example 2 (referred to here as "product X"), and of Example 4 (referred to here as "product XS") were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75g of the solid were added to 1.5 litres of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal litres per hour (and at close to one atmosphere absolute pressure). The reactor was maintained at 70°C by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements. The solid filter-cakes were dried at 110°C and then analysed by X-ray fluorescence spectrometry for elemental composition, by X-ray diffraction for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0074] The results for three different product samples are given in Table 4:\|Table 4Experiment N° ; anhydrous product usedDuration (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %5 Product X3.5420Hydromagnesite31.215.918.20.65961 Product X4.0600Hydromagnesite30.316.418.80.5637 Product XS4.0205Hydromagnesite27.717.219.70.471(1) In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0075] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields, of the order of 60-70% of the total magnesium in the starting material, in a time of 3.5 to 4 hours.	(EP2718230)\|[0001] This invention relates to a process for the mineralization of carbon dioxide from, for example, a gas stream such as the flue gases from an industrial combustion process. The process uses as starting material an alkali metal magnesium silicate and produces magnesium carbonate compounds and silica.\|[0002] In WO 2010/097451 magnesium-comprising silicate hydroxide particles are heated alone to activate the particles, which are then ground to a smaller size and contacted with an aqueous medium (which preferably contains a dissolved bicarbonate salt) and carbon dioxide under low temperature conditions. The solution and small activated particles are then contacted with carbon dioxide at elevated temperatures (preferably at least 140°C, and therefore under pressure to avoid the water simply boiling off).\|[0003] US2009/0202410 similarly discloses contacting an aqueous alkali metal carbonate solution with carbon dioxide to obtain a bicarbonate solution, which is then contacted with a waste material. The mineral may contain, inter alia, a magnesium-containing silicate mineral.\|[0004] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into magnesium silicate hydrate minerals such as serpentine or chlorite (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10)(OH)2).\|[0005] Magnesium silicate rocks constitute an excellent source of basic magnesium which should in theory readily be converted into stable magnesium carbonate compounds by the action of carbon dioxide gas under normal atmospheric conditions. However, in practice, the weathering and carbonation of natural magnesium silicate minerals at the Earth's surface occurs only very slowly. Thus, while the use of magnesium silicates as a source of basic magnesium for the mineralization of carbon dioxide has been proposed as a means to combat the current trend towards increasing carbon dioxide levels in the atmosphere, processes to achieve such mineralization have heretofore been excessively energy-intensive, as well as excessively expensive to set up and operate, and, and thus have not been commercialized. One of the major technical difficulties which renders such processes so expensive to set up and operate is the need to use elevated pressures and temperatures in order to achieve a sufficiently high rate (for industrial purposes) of carbonation of magnesium silicate minerals. Typically, the carbon dioxide gas must first be purified and then compressed to pressures in excess of 70 atmospheres, and then contacted with finely-ground magnesium silicates in a pressure reactor at temperatures of 120-200°C. This requires specialized equipment which is expensive to build and maintain, as well as large amounts of electric power to operate the gas purification and pressurization process as well as to finely grind the magnesium silicate rocks.\|[0006] Although the common magnesium silicate minerals listed above tend to be very "unreactive," (e.g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a "carbonate fusion", is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analysed by standard chemical techniques, thus allowing for total elemental analysis of the rock. The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0007] US 5,085,838A describes a process for reacting an asbestiform material, which may be a magnesium-containing mineral, with an alkaline flux, which may be an alkali metal carbonate, into an environmentally safe glassy material by heating to about 750°C to 1000°C. An X-ray diffraction spectrum attributes one peak to an alkali metal magnesium silicate. The glassy material produced is described as a safe, non-toxic waste, which can be disposed of, or used as a process feed-stock for producing various glassy products.\|[0008] JP2007/146094 describes the use of a water-swelling clay, named as sodium-magnesium silicate, in a detergent composition suitable for cleaning skin. The clay, which is a known material, is not a true alkali metal magnesium silicate, contains lithium as part of its structure and is known by a number of synonyms including lithium magnesium sodium salt, synthetic magnesium lithium silicate and lithium magnesium sodium silicate.\|[0009] The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step.\|[0010] The present invention accordingly provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form or in the form of an alkali metal bicarbonate or carbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.\|[0011] The alkali metal is preferably potassium or, more preferably, sodium.\|[0012] The process is preferably effected at a temperature of 25 to 100°C, more preferably 35 to 80°C. The carbon dioxide may be in the free form in a gas comprising carbon dioxide.\|[0013] The process of the invention can be used to remove carbon dioxide from a gas at a reduced or elevated pressure or, for example, at about atmospheric pressure. The process of the invention may be carried out on a carbon dioxide-containing gas at an absolute pressure generally from 0.5 to 100 bar, preferably from 1 to 20 bar, most preferably at about 1 bar.\|[0014] The gas to be treated may contain from 0.01% to 100% carbon dioxide by volume, preferably from 0.1% to 50%, more preferably from 1% to 40%, and most preferably from 4% to 30%. The gas stream may be a flue gas from an industrial combustion process.\|[0015] The carbon dioxide may also be in the form of an alkali metal carbonate or bicarbonate formed by contacting a gas comprising carbon dioxide with an alkali metal hydroxide or an alkali metal carbonate. The alkali metal carbonate or bicarbonate is preferably produced in the form of an aqueous solution, prepared by reaction between an aqueous solution of an alkali metal hydroxide or carbonate and gaseous carbon dioxide.\|[0016] The alkali metal magnesium silicate is preferably in particulate form, for example a powder, preferably having a Blaine specific surface area of 100 to 800m2/kg, more preferably 200 to 650m2/kg.\|[0017] The process according to the invention is preferably effected with a product comprising alkali metal magnesium silicate. The alkali metal magnesium silicate is preferably prepared by the reaction of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate, or a mixture thereof, with a magnesium silicate. The alkali metal carbonate compound used preferably comprises alkali metal carbonate produced by contacting a gas comprising carbon dioxide with an alkali metal magnesium silicate generally in the presence of water, the alkali metal magnesium silicate being converted into a solution of an alkali metal carbonate plus solid residues comprising magnesium carbonates and a largely amorphous product rich in silica and containing some magnesium by reaction with the carbon dioxide, and the alkali metal carbonate solution being separated and concentrated prior to reaction with the magnesium silicate.\|[0018] The invention also provides a process for the preparation of a product comprising an alkali metal magnesium silicate compound (which compound is preferably of composition R2O•MgO•SiO2, (in which R represents an alkali metal),which process comprises the reaction, at a temperature from 500 to 1100°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 2:1 to 1:2, which reaction produces the product comprising an alkali metal magnesium silicate.\|[0019] The product produced by this process may be in shaped or particulate form.\|[0020] The product may be used to provide a slurry, generally aqueous, comprising an alkali metal magnesium silicate produced by this process.\|[0021] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate expressed as silicon dioxide is preferably from 2:1 to 1:2, more preferably from 3:2 to 2:3, for example 4:3 to 3:4. The ratio is most preferably about 1.\|[0022] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used to prepare the alkali metal magnesium silicate.\|[0023] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0024] The magnesium silicate used in the preparation of the alkali metal magnesium silicate is generally a mineral silicate, for example a rock comprising a high concentration, preferably 20% or more, more preferably 50% or more, of a magnesium silicate of the general formula:\| m(MgO)•t(MeO)•SiO2•xH2O\|wherein Me represents a metal or metals other than magnesium, (such as, for example, calcium and/or iron); m is from 0.5 to 3, preferably from1 to 3, t is less than or equal to 1, and x is from zero to 2.\|[0025] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc iddingsite and hectorite. These minerals may contain substantial quantities of calcium, iron and alkali metals in addition to magnesium and silicon. Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, anthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens. The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0026] The mineral silicate used to prepare the alkali metal magnesium silicate is preferably a basic magnesium silicate. The MgO/SiO2 molar ratio is preferably from 1 to 3. The CaO/SiO2 molar ratio is preferably ≤0.5. The FeO/SiO2 molar ratio is preferably ≤0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≤0.2.\|[0027] The alkali metal carbonate compound used in the preparation of the alkali metal magnesium silicate may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2•2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g. chlorides, sulfates, sulfites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates, nitrites or hydroxides) are present which, at the temperature used to prepare the alkali metal magnesium silicate, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0028] The process used to prepare the alkali metal magnesium silicate is preferably effected at a temperature from 600 to 1000°C, for example 700 to 950°C, more preferably from 800 to 950°C. Heating is generally effected for a few minutes to a few hours, for example from 5 minutes to 24 hours, preferably from 10 minutes to 4 hours.\|[0029] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is slightly below its melting point.\|[0030] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as "R2O" in which R represents an alkali metal) present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt. = 140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt. = 106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0031] The magnesium silicate and alkali metal carbonate compound used to prepare the alkali metal magnesium silicate are preferably in particulate form or in shaped form, e.g. as pellets. Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the preparation of the alkali metal magnesium silicate will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of fine sand (grain size 0.06 to 0.2mm) or, if necessary, ground to a fine powder (grain sizes below 0.06mm). Grain sizes greater than 0.06mm are generally determined by sieving. Grain sizes lower than 0.06mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0032] In one embodiment the process to prepare the alkali metal magnesium silicate is conducted in a moving grate furnace.\|[0033] For example a mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in Figure 1 of the accompanying drawings.\|[0034] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0035] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone ("burning zone") just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate:\| (1) Mg2SiO4 + R2CO3 ⇒ product comprising R2MgSiO4 + CO2↑\|in which R is as hereinbefore defined: R preferably represents sodium.\|[0036] The vertical arrow ↑ after CO2 indicates that the carbon dioxide gas produced by this reaction escapes from the bed and exits with the rest of the exhaust gases. The idealized reaction depicted in equation (1) illustrates the production of a product comprising an alkali metal magnesium silicate by direct reaction of a stoichiometric mixture of forsterite and an alkali metal carbonate. This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 2.6 kJ (i.e. about 0.6 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, the net energy consumption for the overall process will be significant. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0037] In a further embodiment, the preparation of the alkali metal magnesium silicate is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln in a decarbonation step which produces carbon dioxide.\|[0038] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0039] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 40% of the total solids volume. In order to achieve this, it may sometimes be necessary to reduce the R2O/SiO2 ratio of the initial pellet composition to a value substantially below the preferred stoichiometric ratio of 1. The degree of reaction of the magnesium silicate during the process will then also be less than 100% but the effect of this can potentially be mitigated by separating the unreacted magnesium silicate from the reaction products and recycling it together with additional magnesium silicate starting material in the production of a fresh batch of pellets.\|[0040] According to a further feature of the invention the preparation of the alkali metal magnesium silicate is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The R2O/SiO2 ratio may be less than 1 if necessary in order to form substantially stable nodules. The nodules are decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0041] The cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate are then used in a gas scrubbing system designed to remove carbon dioxide from a gas at a reduced or elevated pressure or, for example, at about atmospheric pressure.\|[0042] In one embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are ground in water to make an aqueous suspension or slurry which can be directly injected into a conventional gas scrubbing system, such as a spray tower.\|[0043] In another embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are packed into a vertical column to form a packed bed of pellets through which a gas can be passed from bottom to top, while at the same time a suitably-controlled spray of water is added at the top of the column to ensure that the pellets remain wet. This constitutes a counter-current packed-bed gas absorber column. The flow of water leaving the bottom of this column is collected and treated as described later in more detail. The pellets or nodules used to form this type of packed bed column may be pre-selected for their dimensions and mechanical strength.\|[0044] In both of the above embodiments, the reactions occurring in the gas scrubbing system or gas absorber column are as follows:\| (2) R2MgSiO4(S) + (1+p)CO2(g) + water ⇒ (MgO)•p(CO2)•q(H2O)(s) + solid1 + R2CO3 (aq.)\|Where:\| The terms (s), (g) and (aq.) indicate solid, gas, and aqueous solution, respectively,\| p is > 0 and less than or equal to 1. Preferably, p is greater than or equal to 0.5\| q may be zero but can also take values as high as 3 in some cases.\|[0045] The principal solid products are:\| a magnesium carbonate compound, (MgO)•p(CO2)•q(H2O), which may contain more than one chemical compound, and in which a significant fraction of the carbon dioxide captured from the gas stream is contained in a stable solid form; and\| solid1 which is a largely amorphous solid rich in silica and containing some magnesium.\|[0046] These two principal solid products will generally be intimately mixed.\|[0047] Other minor solid products that may also be present include iron oxides, hydroxides or carbonates, as well as calcium carbonates.\|[0048] The alkali metal carbonate solution resulting from the gas scrubbing process will, if reaction (2) goes to completion, contain all of the alkali metal ions present in the original solid product. It is therefore desirable to separate this alkali metal carbonate solution and extract the alkali metal carbonates in solid form for re-use in the high temperature process according to reaction (1). In principle, this can be done most effectively by a combination of evaporation and crystallization processes, making use of the waste heat available both from the decarbonation reaction (1) and also from the flue gas scrubbing system, (noting that reactions (2) and (3) are both highly exothermic and thus that the gas scrubbing system itself is likely to operate at a higher temperature than the temperature of the flue gases being treated by it, thus producing a hot solution of alkali metal carbonate).\|[0049] Some other salts may be present in the alkali metal carbonate solution due to impurities in the magnesium silicate rocks or the flue gases. The most common impurities are likely to be alkali metal sulfates, sulfites, nitrates and nitrites. Under certain circumstances it may be necessary to separate these salts from the recycled alkali metal carbonate by specialized crystallization and washing procedures.\|[0050] In yet another embodiment of the invention, the cooled decarbonated pellets or nodules, comprising alkali metal magnesium silicate, are crushed, and if necessary ground, to a suitable median particle size. They are then contacted with a solution comprising an alkali metal bicarbonate in, for example, a tank, preferably with some mechanical stirring. The alkali metal bicarbonate solution may originate from a gas scrubbing system designed to capture carbon dioxide from a gas at, for example, atmospheric pressure. Typical reactions between the alkali-metal bicarbonate solution and the solids in this case is shown by the following equations:\| (3) R2MgSiO4(s) + 2(1+p)RHCO3(aq.) + water ⇒ (MgO)•p(CO2)•q(H2O)(s) + solid1 + (2+p)R2CO3 (aq.)\|[0051] The solid1 is as described above.\|[0052] The alkali metal bicarbonate solution (RHCO3(aq.)) used in reaction (3) may be formed by the reaction of the alkali metal carbonate solution (R2CO3(aq.)) produced in reaction (3) with carbon dioxide and water as shown in reaction (4):\| (4) R2CO3 (aq.) + CO2(g) + water ⇒ 2RHCO3(aq.)\|[0053] This reaction can be conducted in a separate gas scrubbing system, thus participating in a closed-loop alkali-carbonate/bicarbonate gas scrubbing system.\|[0054] The reactions described above are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid magnesium carbonate compounds. The magnesium carbonate solid produced may comprise either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or complex magnesium hydroxy-carbonate hydrates, such as artinite (Mg(OH)2•MgCO3•3H2O), or hydromagnesite, (Mg(OH)2•4MgCO3•4H2O), depending on the conditions. All of these precipitated solids, plus the solid1, will in many cases be finer than the unreacted starting material (Mg2SiO4 in this example), and so could be separated from it by sedimentation and then separated from the alkali metal carbonate which remains in solution by filtration. The unreacted starting material (Mg2SiO4 in this case) thus separated can be recycled to the beginning of the process. The alkali metal carbonate solution can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and also recycled to the start of the process. The mixture of magnesium carbonates and largely amorphous product rich in silica and containing some magnesium produced by these reactions is one of the final products of the overall process (and constitutes a feature of the invention) and can be separated for disposal or for use in other processes.\|[0055] One overall object of the process of the invention is to use common magnesium silicate rocks to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable magnesium carbonate compound.\|[0056] An example of a process of the invention which seeks to maximise capture of CO2 from exhaust gases from other industrial processes and to convert it substantially completely into solid magnesium carbonates in an energy-efficient way, not requiring any high-pressure reactors or autoclaves of the type usually required for direct carbonation of magnesium silicates, is shown in Figure 2 (in which solid1 is a largely amorphous product rich in silica and containing some magnesium).\|[0057] Raw materials are prepared to form a mixture of one part of a magnesium silicate (mMgO.SiO2.xH2O) plus another part being a combination of one or more alkali metal carbonate compounds for which the combined composition is represented by the formula (R2O.nCO2.yH2O); the mixture is heated by fuel combustion gases from a burner supplied with fuel and air; the heated mixture reacts to form a product comprising an alkali metal magnesium silicate (R2O.MgO.SiO2) and to release carbon dioxide which mixes with the fuel combustion gases to form exhaust gases with excess carbon dioxide; liquid water is added to the reaction product and the product is wet ground to form a slurry; the slurry is contacted in a gas scrubber with the exhaust gases with excess carbon dioxide produced earlier and with CO2-containing exhaust gases from other processes to absorb carbon dioxide and to produce a slurry comprising magnesium carbonate and silicon dioxide; the slurry is filtered to produce a filtercake comprising magnesium carbonate and a largely amorphous product rich in silica and containing some magnesium; the filter-cake is dried to produce a mixed solid product which is dried; the filtrate comprising alkali metal carbonate compound in solution is dried or crystallized to produce solid alkali metal carbonate compound which is recycled for use as starting material.\|[0058] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0059] The term "pellets" as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0060] Particle size and size distribution when measured by laser granulometry for particle sizes less than about 100µm are measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He-Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.The apparatus is checked before each working session by means of a standard sample (Sifraco C10 silica) for which the particle size distribution is known.\|[0061] Measurements are performed with the following parameters: pump speed 2300rpm and stirrer speed 800rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30s (for possible air bubbles to clear), a measurement is carried out for 15s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0062] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0063] Particle sizes and particle size distributions for particle sizes greater than about 100µm are measured by sieving.\|[0064] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R, m, t, x, p, n, z and y are as initially defined.\|[0065] The following non-limiting Examples illustrate embodiments of the invention.\|EXAMPLE 1\|[0066] Ground olivine sand of composition (Mg0.94Fe0.06)2SiO4 was mixed with a sodium carbonate hydrate powder in a 14:11 mass ratio. 25g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800°C over 2 hours, maintained at 800°C for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table 1:\|Table 1SampleLoss on IgnitionSodium carbonate powder14.97 %Ground olivine sand0.22 %14:11 mix of ground olivine sand + sodium carbonate powder16.69 %\|[0067] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by X-ray diffraction. The reaction products observed by this technique included Na2MgSiO4 and Fe2O3 together with some unreacted olivine and sodium carbonate.\|EXAMPLE 2\|[0068] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. (The molar ratio of this mixture is close to 1). The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900°C. The sample was air-quenched after 1h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851 °C). The measured loss on ignition of all of the samples is presented in the following Table 2 :\|Table 2SampleLoss on IgnitionSodium carbonate14.96 %Olivine0.04 %Olivine + Sodium carbonate23.02 %\|[0069] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by X-ray diffraction and the main phases detected included Na2MgSiO4, together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data.\|EXAMPLE 3\|[0070] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 litres, maintained at 35°C and agitated with a mechanical stirrer operating at 500rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its adsorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in Table 3.\|Table 3Experiment n°Total CO2 captured (mol)Slurry volume (mL)Slurry conc. (g/L)Total solids, (g)CO2 captured, as % of theoretical maximumSlurry additivesTemp. (°C)Duration (h)Solid products detected10,06412605013,0035Na2CO3: 21,15 g/L3524Hydromagnesite20,07242605013,0040Na2CO3: 53,85 g/L3524Hydromagnesite30,13632605013,0075NaHCO3: 53,85 g/L3530Hydromagnesite40,035226011,52,99843526Artinite\|[0071] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite (Mg(OH)2•4MgCO3•4H2O), and in one case artinite (Mg(OH)2•MgCO3•3H2O), which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 4\|[0072] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometre sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950°C), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio. About 5kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950°C for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by X-ray fluorescence spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3, and 33.4% sodium expressed as Na2O. An X-ray diffraction analysis showed the major phase present in the product to be Na2MgSiO4.\|EXAMPLE 5\|[0073] The reaction products of Example 2 (referred to here as "product X"), and of Example 4 (referred to here as "product XS") were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75g of the solid were added to 1.5 litres of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal litres per hour (and at close to one atmosphere absolute pressure). The reactor was maintained at 70°C by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements. The solid filter-cakes were dried at 110°C and then analysed by X-ray fluorescence spectrometry for elemental composition, by X-ray diffraction for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0074] The results for three different product samples are given in Table 4:\|Table 4Experiment N° ; anhydrous product usedDuration (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %5 Product X3.5420Hydromagnesite31.215.918.20.65961 Product X4.0600Hydromagnesite30.316.418.80.5637 Product XS4.0205Hydromagnesite27.717.219.70.471(1) In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0075] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields, of the order of 60-70% of the total magnesium in the starting material, in a time of 3.5 to 4 hours.	Family Number\|(15065813)\|15065813\|Object of Invention\|(EP2532624 A1)\|The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(WO2012168176 A1)\|The present invention seeks to provide a process for the capture of carbon dioxide (C02) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(EP2718230 B1)\|The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(CA2838035 A1)\|The present invention seeks to provide a process for the capture of carbon dioxide (00 2 ) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(CN103582611B B)\|The present invention seeks to provide a method for capturing carbon dioxide ( CO ) by using alkali magnesium silicate which can be made from magnesium silicate rock and which can be carried out , for example , at atmospheric pressure2 ) And / or is capable of removing di directly from a typical industrial flue gas stream without any pre - concentration stepA method for oxidizing carbon . \|(CN103582611 A)\|The present invention seeks to provide a method for capturing carbon dioxide ( CO ) by using alkali magnesium silicate which can be made from magnesium silicate rock and which can be carried out , for example , at atmospheric pressure2 ) And / or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre - concentration step . \|(US20140120022 A1)\|The present invention seeks to provide a process for the capture of carbon dioxide (CO2) by means of a process which may be effected at, for example, atmospheric pressure using an alkali metal magnesium silicate which can be prepared from magnesium silicate rock and/or a process capable of removing carbon dioxide directly from a typical industrial flue gas stream without any pre-concentration step. \|(KR20140045459 A)\| (...) dioxide directly from typical industrial flue gas streams without any preconcentration steps and/or by a process which can be carried out, for example, at atmospheric pressure, using alkali metal magnesium silicate which can be produced from rock magnesium silicate,2) of the present invention.\|Advantages / Prev. Drawbacks\|(CN103582611B B)\|This requires specialized equipment that is expensive to build and maintain , and also requires a large amount of electricity to operate the gas purification and pressurization process and to finely grind the magnesium silicate rock .\|(CN103582611 A)\|This requires specialized equipment that is expensive to build and maintain , and also requires a large amount of electricity to operate the gas purification and pressurization process and to finely grind the magnesium silicate rock .\|	Environmental technology\|Materials, metallurgy	B01D-053/14\|B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-2251/304\|B01D-2251/306\|B01D-2251/402\|B01D-2251/60\|B01D-2251/604\|B01D-2251/606\|B01D-2257/504\|B01D-2258/0283\|C01B-033/22\|C01B-033/32\|C01F-005/24\|Y02C-010/04\|Y02C-010/06\|Y02C-020/40\|Y02P-020/151\|Y02P-020/152		B01D-053/14\|B01D-053/62\|B01D-053/78\|B01D-053/80\|B01D-2251/304\|B01D-2251/306\|B01D-2251/402\|B01D-2251/60\|B01D-2251/604\|B01D-2251/606\|B01D-2257/504\|B01D-2258/0283\|C01B-033/22\|C01B-033/32\|C01F-005/24\|Y02C-010/04\|Y02C-010/06\|Y02C-020/40\|Y02P-020/151\|Y02P-020/152	B01D-053/14\|B01D-053/62\|B01D-053/78\|B01D-053/80\|C01B-033/22\|C01B-033/32\|C01F-005/24	B01D-053/14\|B01D-053/62\|B01D-053/78\|B01D-053/80\|C01B-033/22\|C01B-033/32\|C01F-005/24	PCLO=423331000\|PCLX=423430000	PCLO=423331000 PCLX=423430000	EP2925426\|WO201482996\|WO202662133\|EP2735553;EP2735553\|EP2735555\|WO2024156118\|CN114334032\|CN114390943\|WO2024200557\|DE102023108019\|DE102023108019\|US12258296\|US11718558\|US12110601\|US11839849\|EP4178927\|WO202212795\|CN114728848B\|EP3939945\|AU2013351282;AU2013351282\|US9631257	EP2925426 66131709 WHO=Examiner SELF=Y CAT=X CAT=P CAT=I\|WO201482996 66131709 WHO=Examiner SELF=Y CAT=X CAT=P CAT=I\|WO202662133 118233234 WHO=Examiner SELF=N CAT=X CAT=I\|EP2735553 66070146 WHO=Examiner SELF=N CAT=E\|EP2735555 66070145 WHO=Examiner SELF=N CAT=E\|WO2024156118 104821837 WHO=Examiner SELF=N CAT=A\|CN114334032 99582529 WHO=Examiner SELF=N CAT=A\|CN114390943 92128920 WHO=Examiner SELF=N CAT=A\|WO2024200557 111675593 WHO=Applicant SELF=N\|DE102023108019 111675593 WHO=Examiner SELF=N\|DE102023108019 111675593 WHO=Applicant SELF=N\|US12258296 104821837 WHO=Applicant SELF=N\|US11718558 92777983 WHO=Applicant SELF=N\|US12110601 86698390 WHO=Applicant SELF=N\|US11839849 100984116 WHO=Examiner SELF=N\|EP4178927 98313250 WHO=Applicant SELF=N\|WO202212795 98313250 WHO=Applicant SELF=N\|CN114728848B 93726190 WHO=Examiner SELF=N\|EP3939945 98313250 WHO=Applicant SELF=N\|AU2013351282 66131709 WHO=Examiner SELF=Y\|US9631257 66131709 WHO=Applicant SELF=Y	WO201097451\|WO201097451\|US20090202410\|US20090202410\|US5085838\|US5085838\|WO201097451\|US20090202410\|US5085838\|JP2007146094\|JP2007146094\|JP2007146094\|US20100196235\|US20100196235\|US20100196235\|WO201097451\|WO201097451\|CN101596397\|US20090202410\|US20090202410\|US20090202410\|US20100196235\|CN101356118\|JP2007146094\|JP2007146094\|US5085838\|US5085838\|US5085838	WO201097451 44611783 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|WO201097451 44611783 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|US20090202410 4163858 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|US20090202410 4163858 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|US5085838 42717873 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|US5085838 42717873 WHO=Examiner SELF=N CAT=X CAT=A CAT=Y CAT=I\|WO201097451 44611783 WHO=Examiner SELF=N CAT=X CAT=A CAT=I\|US20090202410 4163858 WHO=Examiner SELF=N CAT=X CAT=A CAT=I\|US5085838 42717873 WHO=Examiner SELF=N CAT=X CAT=A CAT=I\|JP2007146094 32582907 WHO=Examiner SELF=N CAT=X\|JP2007146094 32582907 WHO=Examiner SELF=N CAT=X\|JP2007146094 32582907 WHO=Examiner SELF=N CAT=X\|US20100196235 1841774 WHO=Examiner SELF=N CAT=A\|US20100196235 1841774 WHO=Examiner SELF=N CAT=A\|US20100196235 1841774 WHO=Examiner SELF=N CAT=A\|WO201097451 44611783 WHO=Applicant SELF=N\|WO201097451 44611783 WHO=Applicant SELF=N\|CN101596397 6876258 WHO=Examiner SELF=N\|US20090202410 4163858 WHO=Applicant SELF=N\|US20090202410 4163858 WHO=Applicant SELF=N\|US20090202410 4163858 WHO=Examiner SELF=N\|US20100196235 1841774 WHO=Applicant SELF=N\|CN101356118 6679764 WHO=Examiner SELF=N\|JP2007146094 32582907 WHO=Applicant SELF=N\|JP2007146094 32582907 WHO=Applicant SELF=N\|US5085838 42717873 WHO=Applicant SELF=N\|US5085838 42717873 WHO=Applicant SELF=N\|US5085838 42717873 WHO=Examiner SELF=N		JP2007146094; US20100196235; WO201097451; US20090202410; US5085838\|JP2007146094; US20100196235; WO201097451; US20090202410; US5085838; WO201097451; US20090202410; US5085838; JP2007146094\|\|US5085838; US20090202410; CN101596397; CN101356118\|US5085838; US20090202410; US20100196235; JP2007146094; WO201097451\|\|\|JP2007146094; US20100196235; WO201097451; US20090202410; US5085838	(EP2718230)\|Examiner references\|-See also references of WO 2012168176A1\|\|\|(US9469546)\|Applicant references\|-International Search Report as issued for International Application No. PCT/EP2012/060480, dated Jul. 31, 2012.\|-International Preliminary Report on Patentability as issued for International Application No. PCT/EP2012/060480, dated Dec. 27, 2013.\|\|\|\|\|\|	GRANTED	(EP2718230)\|GRANTED\|(EP2532624)\|LAPSED\|(US9469546)\|LAPSED\|(WO2012/168176)\|LAPSED\|(CN103582611)\|LAPSED\|(HRP20180851)\|LAPSED\|(KR10-2014-0045459)\|LAPSED\|(CA2838035)\|LAPSED	ALIVE	(EP2718230)\|ALIVE\|(EP2532624)\|DEAD\|(US9469546)\|DEAD\|(WO2012/168176)\|DEAD\|(CN103582611)\|DEAD\|(HRP20180851)\|DEAD\|(KR10-2014-0045459)\|DEAD\|(CA2838035)\|DEAD	(EP2718230)\|LEGAL DETAILS FOR EP2718230\|Actual or expected expiration date=2032-06-04\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2012-06-04\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP12727348\|Application date=2012-06-04\|Standardized application number=2012EP-0727348\|Event publication date=2014-03-14\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2014-04-16\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2718230\|Publication stage code=A1\|Publication date=2014-04-16\|Standardized publication number=EP2718230\|Event publication date=2014-04-16\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2014-01-07\|Event publication date=2014-04-16\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2014-09-10\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2017-05-03\|Event code=EP/17Q\|Event indicator=Pos\|Event group=Examination events\|First examination report\|Erster pruefungsbescheid\|Effective date of the event=2017-03-31\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-11\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2017-10-18\|Event code=EP/GRAP\|Event indicator=Pos\|Event group=Examination events\|DESPATCH OF COMMUNICATION OF INTENTION TO GRANT A PATENT\|New entry: communication of intention to grant a patent\|Original code: EPIDOSNIGR1\|Event publication date=2017-11-15\|Event code=EP/INTG\|Event indicator=Pos\|Event group=Examination events\|Announcement of intention to grant\|Effective date of the event=2017-10-19\|Event publication date=2018-02-22\|Event code=EP/GRAS\|Event indicator=Pos\|Event group=Examination events Payment or non-payment notifications\|GRANT FEE PAID\|New entry: payment of fee for grant\|Original code: EPIDOSNIGR3\|Event publication date=2018-03-02\|Event code=EP/GRAJ\|Event group=Examination events\|INFORMATION RELATED TO DISAPPROVAL OF COMMUNICATION OF INTENTION TO GRANT BY THE APPLICANT OR RESUMPTION OF EXAMINATION PROCEEDINGS BY THE EPO DELETED\|Deletion - disapproval of the communication of intention to grant the patent by the applicant or resumption of examination proceedings by the EPO\|Original code: EPIDOSDIGR1\|Event publication date=2018-03-02\|Event code=EP/GRAL\|Event group=Examination events\|INFORMATION RELATED TO PAYMENT OF FEE FOR PUBLISHING/PRINTING DELETED\|Deletion: payment of fee for publishing/printing\|Original code: EPIDOSDIGR3\|Event publication date=2018-04-04\|Event code=EP/INTC\|Event group=Examination events\|Former communication of intention to grant cancelled\|Event publication date=2018-04-11\|Event code=EP/GRAR\|Event indicator=Pos\|Event group=Examination events\|INFORMATION RELATED TO INTENTION TO GRANT A PATENT RECORDED\|New entry: information about intention to grant a patent\|Original code: EPIDOSNIGR71\|Event publication date=2018-04-20\|Event code=EP/GRAA\|Event indicator=Pos\|Event group=Examination events\|(EXPECTED) GRANT\|Original code: 0009210\|Event publication date=2018-05-16\|Event code=EP/INTG\|Event indicator=Pos\|Event group=Examination events\|Announcement of intention to grant\|Effective date of the event=2018-04-11\|Event publication date=2018-05-23\|Event code=EP/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent specification\|Publication country=EP\|Publication number=EP2718230\|Publication stage code=B1\|Publication date=2018-05-23\|Standardized publication number=EP2718230\|Event publication date=2018-05-23\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2018-10-31\|Event code=EP/RAP2\|Event group=Change of name or address Reassignment\|Rights of a patent transferred\|Patentinhaber uebertragung (korr.)\|OWNER:HOLCIM TECHNOLOGY LTD.\|Event publication date=2019-03-29\|Event code=EP/PLBE\|Event indicator=Pos\|Event group=No opposition filed\|NO OPPOSITION FILED WITHIN TIME LIMIT\|Original code: 0009261\|Event publication date=2019-03-29\|Event code=EP/STAANOPP\|Event indicator=Pos\|Event group=No opposition filed Event indicating In Force\|No opposition filed within time limit\|Original code: STAA\|Event publication date=2019-05-01\|Event code=EP/26N\|Event indicator=Pos\|Event group=No opposition filed Event indicating In Force\|No opposition filed\|Kein einspruch eingelegt\|Effective date of the event=2019-02-26\|MEMBER STATE LEGAL DETAILS FOR AL\|Actual or expected expiration date=2019-11-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=AL\|Event publication date=2019-11-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=AL\|MEMBER STATE LEGAL DETAILS FOR AT\|Actual or expected expiration date=2032-06-04\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=AT Corresponding appl: AT1001087\|Event publication date=2018-06-15\|Event code=EP/REG\|Event code=AT/REF\|Event indicator=Pos\|Event group=Entry into national phase\|Reference to a national code\|Reference to at number (ep patent enters austrian national phase)\|Nennung der e-nummer (EP patent tritt in at nationale phase ein)\|Effective date of the event=2018-06-15\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2018-08-30\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-08-30\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2019-09-15\|Event code=EP/REG\|Event code=AT/PC\|Event group=Change of name or address Reassignment\|Reference to a national code\|Change of the owner\|Aenderung an der person des patentinhabers\|OWNER:HOLCIM TECHNOLOGY LTD, CH\|Effective date of the event=2019-08-02\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2020-02-15\|Event code=EP/REG\|Event code=AT/MM01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Lapse because of not paying annual fees\|Loeschung wegen nichtzahlung der jaehrlichen gebuehr\|Effective date of the event=2019-06-04\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2020-05-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=AT\|Event publication date=2021-07-15\|Event code=EP/REG\|Event code=AT/UEP\|Event indicator=Pos\|Event group=Examination events Entry into national phase\|Reference to a national code\|Publication of translation of european patent specification\|Uebersetzung der europaeischen patentschrift ausgegeben\|Effective date of the event=2018-05-23\|Corresponding cc:\|Designated or member state=AT\|MEMBER STATE LEGAL DETAILS FOR BE\|Actual or expected expiration date=2018-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BE\|Event publication date=2019-03-06\|Event code=EP/REG\|Event code=BE/MM\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|LAPSED BECAUSE OF NON-PAYMENT OF THE ANNUAL FEE\|Effective date of the event=2018-06-30\|Corresponding cc:\|Designated or member state=BE\|Event publication date=2019-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=BE\|MEMBER STATE LEGAL DETAILS FOR BG\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BG\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=BG\|MEMBER STATE LEGAL DETAILS FOR CH\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2018-05-31\|Event code=EP/REG\|Event code=CH/EP\|Event indicator=Pos\|Event group=Entry into national phase\|Reference to a national code\|EUROPEAN PATENT TAKES EFFECT AS A NATIONAL PATENT IN CH/LI\|Wirkung des europäischen patents als nationales patent in ch/li tritt ein\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2019-01-31\|Event code=EP/REG\|Event code=CH/PL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent ceased\|Loeschung/radiation/radiazion\|Corresponding cc:\|Designated or member state=CH\|Event publication date=2019-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=CH\|MEMBER STATE LEGAL DETAILS FOR CY\|Actual or expected expiration date=2020-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CY\|Event publication date=2020-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=CY\|MEMBER STATE LEGAL DETAILS FOR CZ\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CZ\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=CZ\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2020-01-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE Corresponding appl: DE602012046594\|Event publication date=2017-09-06\|Event code=EP/REG\|Event code=DE/R079\|Event group=Corrections\|Reference to a national code\|Amendment of ipc main class\|Aenderung der IPC hauptklasse\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2017-09-06\|Event code=EP/REG\|Event code=DE/R079\|Event group=Corrections\|Reference to a national code\|Amendment of ipc main class\|Aenderung der IPC hauptklasse\|Previous main class: C01B0033220000\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-06-21\|Event code=EP/REG\|Event code=DE/R096\|Event indicator=Pos\|Event group=Examination events\|Reference to a national code\|DPMA publication of mentioned EP patent grant\|Veroeffentlichung eines hinweises auf die ep-patenterteilung durch das dpma\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-06-27\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-06-27\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-09-20\|Event code=EP/REG\|Event code=DE/R082\|Event group=Examination events\|Reference to a national code\|Change of representative\|Aenderung des vertreters\|REPRESENTATIVE:BEETZ & PARTNER MBB PATENT- UND RECHTSANWAELTE, DE\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-09-20\|Event code=EP/REG\|Event code=DE/R081\|Event group=Examination events Reassignment\|Reference to a national code\|Change of applicant/patentee\|Aenderung des anmelders/inhabers\|Former owner: LAFARGE, PARIS, FR\|OWNER:HOLCIM TECHNOLOGY LTD., CH\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2018-09-20\|Event code=EP/REG\|Event code=DE/R082\|Event group=Examination events\|Reference to a national code\|Change of representative\|Aenderung des vertreters\|REPRESENTATIVE:BEETZ & PARTNER MBB PATENTANWAELTE, DE\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2019-02-26\|Event code=EP/REG\|Event code=DE/R097\|Event indicator=Pos\|Event group=No opposition filed\|Reference to a national code\|No opposition filed against granted patent, or EPO opposition proceedings concluded without decision\|Gegen die patenterteilung wurde kein einspruch erhoben, bzw. einspruchsverfahren ist beim epa ohne entscheidung abgeschlossen\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2020-01-01\|Event code=EP/REG\|Event code=DE/R119\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Application deemed withdrawn, or ip right lapsed, due to non-payment of renewal fee\|Die anmeldung gilt als zurueckgenommen wegen nichtzahlung der jahresgebuehr / schutzrecht ist wegen nichtzahlung der jahresgebuehr verfallen\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2020-05-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR DK\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DK\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=DK\|MEMBER STATE LEGAL DETAILS FOR EE\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EE\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=EE\|MEMBER STATE LEGAL DETAILS FOR ES\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=ES\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=ES\|MEMBER STATE LEGAL DETAILS FOR FI\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=FI\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=FI\|MEMBER STATE LEGAL DETAILS FOR FR\|Actual or expected expiration date=2020-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2018-06-26\|Event code=EP/REG\|Event code=FR/PLFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications Restitution or restoration\|Reference to a national code\|Fee payment\|Derniere annuite payee\|Annual fees payment date=2018-06-26\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2018-06-26\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-06-26\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=FR\|Event publication date=2020-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=FR\|MEMBER STATE LEGAL DETAILS FOR GB\|Actual or expected expiration date=2018-08-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2018-05-23\|Event code=EP/REG\|Event code=GB/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patent granted\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2018-08-23\|Event code=EP/GBPC\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|GB: European patent ceased through non-payment of renewal fee\|Effective date of the event=2018-08-23\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2019-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=GB\|MEMBER STATE LEGAL DETAILS FOR GR\|Actual or expected expiration date=2020-05-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GR Corresponding appl: GR20180401871\|Event publication date=2018-07-19\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-07-19\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=GR\|Event publication date=2019-01-25\|Event code=EP/REG\|Event code=GR/EP\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|Ep patent validated in greece\|Effective date of the event=2019-01-09\|Corresponding cc:\|Designated or member state=GR\|Event publication date=2020-05-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=GR\|MEMBER STATE LEGAL DETAILS FOR HRP20180851\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HR Corresponding appl: HRP20180851\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2018HR-0000851\|Corresponding cc:\|Designated or member state=HR Corresponding pat: HRP20180851\|Publication stage code in the designated or member state=T1\|Publication date in the designated or member state=2018-06-29\|Publication number in the designated or member state=HRP20180851\|Event publication date=2018-05-29\|Event code=EP/REG\|Event code=HR/TUEP\|Event group=Administrative notifications\|Reference to a national code\|REQUEST FOR EP VALIDATION RECEIVED\|Uredan zahtjev za upis (prosirenog) europskog patenta\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2018-06-11\|Event code=EP/REG\|Event code=HR/ODRP\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|Reference to a national code\|RENEWAL FEE FOR THE MAINTENANCE OF A PATENT\|Odrzavanje patenta u vrijednosti\|Annual fees payment date=2018-06-11\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2018-06-11\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-06-11\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2018-06-29\|Event code=EP/REG\|Event code=HR/T1PR\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|EP PATENT VALIDATED IN CROATIA\|Ep patent validiran u hrvatskoj\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2019-02-05\|Event code=EP/REG\|Event code=HR/PPPP\|Event group=Reassignment\|Reference to a national code\|TRANSFER OF RIGHTS\|Prijenos prava\|OWNER:HOLCIM TECHNOLOGY LTD, CH\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2019-06-04\|Event code=EP/REG\|Event code=HR/PBON\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Reference to a national code\|LAPSE DUE TO NON-PAYMENT OF RENEWAL FEE\|Prestanak vrijednosti patenata zbog neodrzavanja\|Effective date of the event=2019-06-04\|Corresponding cc:\|Designated or member state=HR\|Event publication date=2020-05-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=HR\|MEMBER STATE LEGAL DETAILS FOR HU\|Actual or expected expiration date=2020-05-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HU\|Event publication date=2020-05-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO\|Corresponding cc:\|Designated or member state=HU\|MEMBER STATE LEGAL DETAILS FOR IE\|Actual or expected expiration date=2019-03-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2018-06-13\|Event code=EP/REG\|Event code=IE/FG4D\|Event indicator=Pos\|Event group=Event indicating In Force\|Reference to a national code\|European patents granted designating Ireland\|European patent granted\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2019-03-20\|Event code=EP/REG\|Event code=IE/MM4A\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent lapsed\|Corresponding cc:\|Designated or member state=IE\|Event publication date=2019-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=IE\|MEMBER STATE LEGAL DETAILS FOR IS\|Actual or expected expiration date=2020-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IS\|Event publication date=2020-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IS\|MEMBER STATE LEGAL DETAILS FOR IT\|Actual or expected expiration date=2020-05-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2018-08-22\|Event code=EP/PGFP\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Annual fee paid to national office [announced from national office to EPO]\|Postgrant: annual fees paid to national office\|Annual fees payment date=2018-08-22\|Year of payment of annual fees=7\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2020-05-01\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=IT\|MEMBER STATE LEGAL DETAILS FOR LI\|Actual or expected expiration date=2019-04-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LI\|Event publication date=2019-04-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LI\|MEMBER STATE LEGAL DETAILS FOR LT\|Actual or expected expiration date=2018-10-10\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2018-10-10\|Event code=EP/REG\|Event code=LT/MG4D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Invalidated european patent\|Europos patentai, laikomi ab initio negaliojanciais\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LT\|MEMBER STATE LEGAL DETAILS FOR LU\|Actual or expected expiration date=2019-03-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LU\|Event publication date=2019-03-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LU\|MEMBER STATE LEGAL DETAILS FOR LV\|Actual or expected expiration date=2018-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LV\|Event publication date=2018-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LV\|MEMBER STATE LEGAL DETAILS FOR MC\|Actual or expected expiration date=2019-03-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MC\|Event publication date=2019-03-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MC\|MEMBER STATE LEGAL DETAILS FOR MK\|Actual or expected expiration date=2020-06-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MK\|Event publication date=2020-06-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=MK\|MEMBER STATE LEGAL DETAILS FOR MT\|Actual or expected expiration date=2020-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MT\|Event publication date=2020-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=MT\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=2018-05-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2018-09-26\|Event code=EP/REG\|Event code=NL/MP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent voided (invalid in the netherlands as no translation has been filed)\|Effective date of the event=2018-05-23\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2018-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NL\|MEMBER STATE LEGAL DETAILS FOR NO\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NO\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NO\|MEMBER STATE LEGAL DETAILS FOR PL\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PL\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PL\|MEMBER STATE LEGAL DETAILS FOR PT\|Actual or expected expiration date=2020-05-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PT\|Event publication date=2020-05-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PT\|MEMBER STATE LEGAL DETAILS FOR RO\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RO\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RO\|MEMBER STATE LEGAL DETAILS FOR RS\|Actual or expected expiration date=2018-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RS\|Event publication date=2018-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RS\|MEMBER STATE LEGAL DETAILS FOR SE\|Actual or expected expiration date=2018-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2018-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SE\|MEMBER STATE LEGAL DETAILS FOR SI\|Actual or expected expiration date=2019-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SI\|Event publication date=2019-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SI\|MEMBER STATE LEGAL DETAILS FOR SK\|Actual or expected expiration date=2019-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SK\|Event publication date=2019-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SK\|MEMBER STATE LEGAL DETAILS FOR SM\|Actual or expected expiration date=2019-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SM\|Event publication date=2019-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SM\|MEMBER STATE LEGAL DETAILS FOR TR\|Actual or expected expiration date=2020-03-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=TR\|Event publication date=2020-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=TR\|(EP2532624)\|LEGAL DETAILS FOR EP2532624\|Actual or expected expiration date=2017-07-15\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-06-07\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP11305696\|Application date=2011-06-07\|Standardized application number=2011EP-0305696\|Event publication date=2012-12-11\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2012-12-12\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2532624\|Publication stage code=A1\|Publication date=2012-12-12\|Standardized publication number=EP2532624\|Event publication date=2012-12-12\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2012-12-12\|Event code=EP/AX\|Event indicator=Pos\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT\|Request for extension of the european patent to\|Designated contracting states=BA ME\|Event publication date=2013-07-24\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2013-06-12\|Event publication date=2013-07-24\|Event code=EP/RBV\|Event indicator=Pos\|Event group=Designated states Corrections\|Designated contracting states (correction):\|Benannte vertragsstaaten (korr.)\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2017-05-03\|Event code=EP/17Q\|Event indicator=Pos\|Event group=Examination events\|First examination report\|Erster pruefungsbescheid\|Effective date of the event=2017-04-03\|Event publication date=2017-12-22\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2018-01-24\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2017-07-15\|(US9469546)\|LEGAL DETAILS FOR US9469546\|Actual or expected expiration date=2020-11-23\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US14123987\|Application date=2012-06-04\|Standardized application number=2012US-14123987\|Event publication date=2012-06-04\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:BERNS, DANIEL J\|Event publication date=2012-06-04\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2012-06-04\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 035112-0428430\|Event publication date=2012-06-04\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 909\|Event publication date=2012-06-04\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2012-06-04\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2013-12-05\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:GARTNER, ELLIS;PISCH, ALEXANDER;SIGNING DATES FROM 20131122 TO 20131126\|Reel/frame:031720/0728\|OWNER:LAFARGE, FRANCE\|Event publication date=2013-12-05\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2013-12-05\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2013-12-05\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2014-01-10\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2014-01-24\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2014-01-24\|Event code=US/M903\|Event indicator=Pos\|Event group=Examination events OAO\|Notice of DO/EO Acceptance Mailed\|Event publication date=2014-02-26\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2014-05-01\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20140120022\|Publication stage code=A1\|Publication date=2014-05-01\|Standardized publication number=US20140120022\|Event publication date=2014-05-01\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2015-11-15\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2015-11-19\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2015-11-19\|R4R=102b\|RJST=non-final\|Rejected claims 1-12\|RJCT=WO2010097451\|Event publication date=2015-11-19\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2015-11-19\|R4R=112b\|RJST=non-final\|Rejected claims 5-8 and 10-12; 5; 10\|Event publication date=2016-02-19\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2016-06-02\|Event code=US/EXET\|Event group=Examination events OAO INT\|Interview Summary - Examiner Initiated - telephonic\|Event publication date=2016-06-13\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2016-06-17\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2016-09-13\|Event code=US/NOARR\|Event group=Examination events\|Response to Reasons for Allowance\|Event publication date=2016-09-13\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2016-09-13\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2016-09-14\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2016-09-28\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2016-10-18\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US09469546\|Publication stage code=B2\|Publication date=2016-10-18\|Standardized publication number=US9469546\|Event publication date=2016-10-18\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 283 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=283\|Event publication date=2019-01-18\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignor:LAFARGE\|Reel/frame:048061/0707\|OWNER:HOLCIM TECHNOLOGY LTD, SWITZERLAND\|Effective date of the event=2018-12-10\|Event publication date=2019-10-29\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2020-06-08\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2020-10-18\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2020-10-18\|Event publication date=2020-11-23\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2020-11-23\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|Event publication date=2023-10-31\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|(WO2012/168176)\|LEGAL DETAILS FOR WO2012/168176\|Actual or expected expiration date=2014-12-07\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOEP2012/060480\|Application date=2012-06-04\|Standardized application number=2012WO-EP60480\|Event publication date=2012-12-13\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2012/168176\|Publication stage code=A1\|Publication date=2012-12-13\|Standardized publication number=WO2012168176\|Event publication date=2014-12-07\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR CA2838035\|Actual or expected expiration date=2020-08-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA2838035\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2012CA-2838035\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA2838035\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2012-12-13\|Publication number in the designated or member state=CA2838035\|Event publication date=2013-12-03\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=CA\|Event publication date=2020-11-07\|Event code=CA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR CN103582611\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN201280027687\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2012CN-80027687\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN103582611\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2014-02-12\|Publication number in the designated or member state=CN103582611\|Event publication date=2020-05-22\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2013-12-09\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2013-12-09\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP2718230\|Actual or expected expiration date=2032-06-04\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP12727348\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2012EP-0727348\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2718230\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2014-04-16\|Publication number in the designated or member state=EP2718230\|Event publication date=2013-02-06\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2013-11-20\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2019-05-01\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR HRP20180851\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=HR Corresponding appl: HRP20180851\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2018HR-0000851\|Corresponding cc:\|Designated or member state=HR Corresponding pat: HRP20180851\|Publication stage code in the designated or member state=T1\|Publication date in the designated or member state=2018-06-29\|Publication number in the designated or member state=HRP20180851\|Event publication date=2018-06-29\|Event code=HR/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=HR\|MEMBER STATE LEGAL DETAILS FOR KR10-2014-0045459\|Actual or expected expiration date=2017-07-05\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=KR Corresponding appl: KR20137035129\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2013KR-7035129\|Corresponding cc:\|Designated or member state=KR Corresponding pat: KR10-2014-0045459\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2014-04-16\|Publication number in the designated or member state=KR20140045459\|Event publication date=2013-12-31\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=KR\|Event publication date=2017-07-05\|Event code=KR/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=KR\|MEMBER STATE LEGAL DETAILS FOR US20140120022\|Actual or expected expiration date=2020-11-23\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=US Corresponding appl: US14123987\|Application date in the designated or member state=2012-06-04\|Application number in the designated or member state=2012US-14123987\|Corresponding cc:\|Designated or member state=US Corresponding pat: US20140120022\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2014-05-01\|Publication number in the designated or member state=US20140120022\|Event publication date=2013-12-05\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=US\|Event publication date=2023-10-31\|Event code=US/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=US\|(CN103582611)\|LEGAL DETAILS FOR CN103582611\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201280027687\|Application date=2012-06-04\|Standardized application number=2012CN-80027687\|Event publication date=2014-02-12\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN103582611\|Publication stage code=A\|Publication date=2014-02-12\|Standardized publication number=CN103582611\|Event publication date=2014-02-12\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2014-06-04\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2017-03-08\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN103582611\|Publication stage code=B\|Publication date=2017-03-08\|Standardized publication number=CN103582611B\|Event publication date=2017-03-08\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2019-03-12\|Event code=CN/TR01\|Event group=Change of name or address Reassignment\|Transfer of patent right\|FORMER APPLICANT:Lafarge Holcim Ltd FORMER APPLICANT:LAFARGE SA APPLICANT:HOLCIM TECHNOLOGY LTD. APPLICANT:Lafarge Holcim Ltd\|Effective date of the event=2019-02-20\|Event publication date=2020-05-22\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee\|Effective date of the event=2019-06-04\|(HRP20180851)\|LEGAL DETAILS FOR HRP20180851\|Actual or expected expiration date=2019-06-04\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=HR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=HR HRP20180851\|Application date=2012-06-04\|Standardized application number=2018HR-0000851\|Event publication date=2018-06-29\|Event code=HR/T1\|Event indicator=Pos\|Event group=Event indicating In Force\|Translation of the claims of an EP into Croatian\|Publication country=HR\|Publication number=HRP20180851\|Publication stage code=T1\|Publication date=2018-06-29\|Standardized publication number=HRP20180851\|Event publication date=2019-06-04\|Event code=HR/REG\|Event code=HR/PBON\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Reference to a national code\|LAPSE DUE TO NON-PAYMENT OF RENEWAL FEE\|Prestanak vrijednosti patenata zbog neodrzavanja\|Effective date of the event=2019-06-04\|(KR10-2014-0045459)\|LEGAL DETAILS FOR KR10-2014-0045459\|Actual or expected expiration date=2017-07-05\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=KR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=KR KR20137035129\|Application date=2012-06-04\|Standardized application number=2013KR-7035129\|Event publication date=2014-04-16\|Event code=KR/A\|Event group=Examination events\|Published application\|Publication country=KR\|Publication number=KR10-2014-0045459\|Publication stage code=A\|Publication date=2014-04-16\|Standardized publication number=KR20140045459\|Event publication date=2017-07-05\|Event code=KR/WITN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Withdrawal due to no request for examination\|(CA2838035)\|LEGAL DETAILS FOR CA2838035\|Actual or expected expiration date=2020-08-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-06-04\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2838035\|Application date=2012-06-04\|Standardized application number=2012CA-2838035\|Event publication date=2012-12-13\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2838035\|Publication stage code=A1\|Publication date=2012-12-13\|Standardized publication number=CA2838035\|Event publication date=2020-11-07\|Event code=CA/FZDE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Dead\|Effective date of the event=2020-08-31	(EP2718230)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP2532624)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP2532624)\|Extension States: ME, BA\|(WO2012/168176)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2012/168176)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2012/168176)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2012/168176)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2012/168176)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, RW, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KM, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PE, PG, PH, PL	(EP2718230)\|EP; AT\|(WO2012/168176)\|EP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=9ru+nrv5joioDTVwA2ochGkyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP2718230&ekey=898&xpn=EP2718230&kind=B1	https://register.epo.org/application?number=EP12727348	https://permalink.orbit.com/RenderStaticFirstPage?XPN=92uohvSKJgbVNtz%252BuaPnF3fDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	EP	(WO2012/168176)\|FR\|(EP2532624)\|FR	(WO2012/168176)\|NAME=LAFARGE 61 rue des Belles Feuilles F-75116 Paris , COUNTRY=FR\|(EP2532624)\|NAME=LAFARGE 61, rue des Belles Feuilles , CITY=75116 Paris , COUNTRY=FR , REG=100163084	(EP2718230)\|AT\|(EP2718230)\|FR\|(EP2532624)\|FR\|\|(WO2012/168176)\|FR\|\|\|\|(CA2838035)\|CA	(EP2718230)\|NAME=Keschmann, Marc;Haffner und Keschmann Patentanwälte GmbH Schottengasse 3a , CITY=1014 Wien , COUNTRY=AT , REG=101393339\|(EP2718230)\|NAME=Mérigeault, Shona;Lafarge Département Propriété Industrielle (DPI) 95 Rue du Montmurier BP 9 , CITY=38291 Saint Quentin Fallavier Cedex , COUNTRY=FR , REG=101004378\|(EP2532624)\|NAME=Mérigeault, Shona;Lafarge Département Propriété Industrielle (DPI) 95 Rue du Montmurier BP 9 , CITY=38291 Saint Quentin Fallavier Cedex , COUNTRY=FR , REG=101004378\|(US9469546)\|NAME=Pillsbury Winthrop Shaw Pittman LLP\|(WO2012/168176)\|NAME=MERIGEAULT, Shona LAFARGE Département Propriété Intellectuelle (DPI) 95 rue du Montmurier - BP9 F-38291 Saint Quentin Fallavier Cedex , COUNTRY=FR\|(CN103582611)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314NAME=ZHU HUINING;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(CN103582611)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314NAME=ZHU HUINING;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(KR10-2014-0045459)\|NAME=KOREANA PATENT FIRM , REG=920011000013\|(CA2838035)\|NAME=NORTON ROSE FULBRIGHT CANADA LLP/S.E.N.C.R.L., S.R.L. , COUNTRY=CA	(EP2718230)\|FR; FR\|(EP2718230)\|FR; FR\|(EP2532624)\|FR; FR\|(US9469546)\|FR; FR\|(US20140120022)\|FR; FR\|(WO2012/168176)\|FR; FR\|(CN103582611)\|FR\|\|\|\|(CA2838035)\|FR; FR	(EP2718230)\|NAME=GARTNER, Ellis 42 rue Jean-Marc Bernard, CITY=F-69003 Lyon, COUNTRY=FR \|NAME=PISCH, Alexander Le Clos des Vignes 15 Traverse du Gamay, CITY=F-38090 Villefontaine, COUNTRY=FR\|(EP2718230)\|NAME=GARTNER, Ellis 42 rue Jean-Marc Bernard, CITY=F-69003 Lyon, COUNTRY=FR \|NAME=PISCH, Alexander Le Clos des Vignes 15 Traverse du Gamay, CITY=F-38090 Villefontaine, COUNTRY=FR\|(EP2532624)\|NAME=Gartner, Ellis 42 rue Jean-Marc Bernard, CITY=69003 LYON, COUNTRY=FR \|NAME=Pisch, Alexander Le clos des vignes 15 Traverse du Gamay, CITY=38090 Villefontaine, COUNTRY=FR\|(US9469546)\|NAME=Gartner Ellis, CITY=Lyons, COUNTRY=FR \|NAME=Pisch Alexander, CITY=Villefontaine, COUNTRY=FR\|(US20140120022)\|NAME=Gartner Ellis, CITY=Lyon, COUNTRY=FR \|NAME=Pisch Alexander, CITY=Villefontaine, COUNTRY=FR\|(WO2012/168176)\|NAME=GARTNER, Ellis 42 rue Jean-Marc Bernard F-69003 Lyon, COUNTRY=FR \|NAME=PISCH, Alexander Le Clos des Vignes 15 Traverse du Gamay F-38090 Villefontaine, COUNTRY=FR\|(CN103582611)\|NAME=E. Goldner Paris, FRA, CITY=Paris, STATE=Paris , COUNTRY=FR \|NAME=PISCH ALEXANDER\|(CN103582611)\|NAME=GARTNER ELLIS\|NAME=PISCH ALEXANDER\|(HRP20180851)\|NAME=Gartner, Ellis\|NAME=Pisch, Alexander\|(KR10-2014-0045459)\|NAME=GARTNER ELLIS\|NAME=PISCH ALEXANDER\|(CA2838035)\|NAME=GARTNER, ELLIS, COUNTRY=FR \|NAME=PISCH, ALEXANDER, COUNTRY=FR	(WO2012/168176)\|2\|(EP2718230)\|2\|(CN103582611)\|2\|(US9469546)\|2\|(KR10-2014-0045459)\|2\|(CA2838035)\|2\|(EP2532624)\|2	3	8			(EP2718230)\|WO2012/168176\|(US9469546)\|WO2012/168176\|(CN103582611)\|WO2012/168176\|(HRP20180851)\|WO2012/168176\|(KR10-2014-0045459)\|WO2012/168176\|(CA2838035)\|WO2012/168176	(HRP20180851)\|EP12727348	(EP2718230)\|Number of Claims: NCL=9\|\|(EP2532624)\|Number of Claims: NCL=10\|Primary examiner: Hartlieb, Ariane\|\|(US9469546)\|Number of Claims: NCL=5\|Number of Drawings: NDR=1\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=283\|Primary examiner: Berns Daniel\|Art Unit.: ART =1736\|\|(US20140120022)\|Number of Claims: NCL=12\|Number of Drawings: NDR=1\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Berns Daniel\|Art Unit.: ART =1736\|\|(WO2012/168176)\|Number of Claims: NCL=12\|Extended kind: EXTK=x\|\|(CN103582611)\|Number of Claims: NCL=8\|Gazette date: GAZDATE=2017-03-08\|Gazette number: GAZNUM=33-10\|Substantial examination effective date: 20140604 Examination duration: 33 months\|Number of Pages: NPAGES=13\|Primary examiner: Jiang Shuai\|Primary examiner: 江帅\|\|(CN103582611)\|Number of Claims: NCL=12\|Gazette date: GAZDATE=2014-02-12\|Gazette number: GAZNUM=30-07\|Substantial examination effective date: 20140604 Examination duration: 33 months\|Number of Pages: NPAGES=13\|Primary examiner: Jiang Shuai\|Primary examiner: 江帅\|\|(KR10-2014-0045459)\|Number of Claims: NCL=12\|Number of Pages: NPAGES=13\|\|(CA2838035)\|Number of Claims: NCL=10\|Number of Pages: NPAGES=18\|	(US9469546)\|Previous publication: US20140120022 A1 2014-05-01 [US20140120022]\|(CN103582611)\|Previous publication: CN103582611 A 2014-02-12 [CN103582611]	(EP2718230)\|ENGLISH (ENG)	(HRP20180851)\|Patent\|(EP2718230)\|Patent\|(CN103582611B)\|Patent\|(US9469546)\|Patent\|(US20140120022)\|Patent\|(EP2718230)\|Patent\|(KR20140045459)\|Patent\|(CN103582611)\|Patent\|(CA2838035)\|Patent\|(WO2012168176)\|Patent\|(EP2532624)\|Patent	Titre: (EP2718230)\|Process for the mineralization of carbon dioxide Résumé: (EP2718230)\|The invention provides a process for the mineralization of carbon dioxide to form a magnesium carbonate compound, which process comprises contacting the carbon dioxide, in the free form, or in the form of an alkali metal carbonate or bicarbonate, with an alkali metal magnesium silicate to produce the magnesium carbonate compound.	39	Abstract	gpt-4o-mini	yes	The process described involves the mineralization of CO₂ to form magnesium carbonate, which aligns with the goal of enhanced weathering and carbon sequestration using silicate minerals.
40	US63/256,986P\|US63/281,575P\|US63/298,412P	EP22157366	EP4166641	104628663	EP4166641 A1 2023-04-19 [EP4166641]	2021-10-18\|2021-11-19\|2022-01-11	2022-02-17	2023-04-19		(EP4166641)\|2023-10-20	(EP4166641)\|Systems and methods for processing olivine	(EP4166641)\|The present disclosure provides a system for processing olivine. The system may comprise a reactor for accelerating olivine weathering. The reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering.	PROJECT VESTA PBC	(EP4166641)\|Project Vesta, PBC ([US])	ROMANIELLO STEPHEN JUSTIN\|LEY BRIAN DAVID\|ANDREWS MARGARET GRACE\|WALWORTH NATHAN GERARD\|ISHOEY THOMAS\|GREEN TOM COXETER\|MONTSERRAT FRANCESC	(EP4166641)\|ROMANIELLO, Stephen Justin\|LEY, Brian David\|ANDREWS, Margaret Grace\|WALWORTH, Nathan Gerard\|ISHOEY, Thomas\|GREEN, Tom Coxeter\|MONTSERRAT, Francesc	(EP4166641)\|Hamer, Christopher K. ([GB])\|Reg. Nb: 100052783	(EP4166641)\|The systems and methods disclosed herein may enable efficient processing and deployment of olivine for purposes of CO2 capture in marine environments.\|The systems and methods of the present disclosure enable the acceleration of Earth's natural carbon removal method of rock weathering, through the extraction, processing (e.g., crushing and/or grinding), and transportation of volcanic mineral olivine to coastlines for dispersal or distribution.\|This may be a good reference to understand regulations for effluent from microbial processes.\|Although enhanced silicate weathering may be implemented in some instances, none of the prior work has [8] recognized and provided methods for the manufacture of engineered carbon-negative materials with specific suitable colors, grainsize, density, and reactivity required to meet specific regulatory, aesthetic, and engineering requirement for coastal engineering.\|In some embodiments, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process.\|Recognized herein are various limitations with current weathering methods, which may (i) involve long lead times and labor intensive procedures, (ii) impact ecological conditions (e.g., increasing water turbidity), and (iii) handling/processing of minerals that can pose additional ecological and health hazards via the possible ingestion, contact, or inhalation of fine grain of olivine mineral dust.\|	(EP4166641)\|1. A system for processing olivine, comprising:a reactor for accelerating olivine weathering, wherein the reactor comprises one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate said olivine weathering.\|7. A method, comprising: (a) generating one or more models for determining or predicting olivine dissolution, carbon sequestration, or one or more reaction fluxes associated with a dissolution of olivine in a target environment; (b) obtaining one or more sensor measurements at the target environment; (c) validating and/or updating the one or more models based on the one or more sensor measurements; and (d) using the one or more validated and/or updated models to determine or predict (i) olivine dissolution, (ii) carbon sequestration, and (iii) the one or more reaction fluxes in the target environment.\|	(EP4166641)\|The present application relates generally to using olivine to achieve enhanced weathering and increase CO2 uptake on accelerated timescales. In one aspect, the present disclosure provides systems and methods for accelerating weathering. In another aspect, the present disclosure provides a bioreactor configured to accelerate dissolution of olivine for weathering applications. In a further aspect, the present disclosure provides systems and methods for enhancing material properties of olivine. For example, the present disclosure provides a way to optimize the surface area effect of fine olivine grains by utilizing a binding process to bind or encapsulate the olivine fines into pellets of a larger effective grain size which can be more safely handled and distributed in the environment.\|The present disclosure provides a system for processing olivine.\|The present invention relates to a system for processing olivine. More specifically, the present invention relates to a system for processing olivine wherein the system comprises a reactor for accelerating olivine weathering, more particularly, the reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering.\|	(EP4166641)\|PROCESSING OLIVINE(100,6)\|OLIVINE DISSOLUTION(95,46)\|ENZYMATIC ACCELERANT(86,8)\|VOLCANIC MINERAL OLIVINE(76,2)\|TARGET ENVIRONMENT(73,7)\|OLIVINE(71,177)\|MODEL VALIDATION(71,1)\|ENHANCED SILICATE WEATHERING(65,1)\|ACCELERATED TIMESCALE(63,1)\|PELLETIZED OLIVINE AGGREGATE(60,2)\|OLIVINE GRAIN(57,16)\|MICROBE(56,4)\|OLIVINE DEPLOYMENT(55,2)\|DISSOLUTION ACCELERATOR(55,1)\|REACTOR(53,11)\|WEATHERING(52,2)\|FINE OLIVINE GRAIN(50,2)\|OLIVINE MINERAL DUST(48,1)\|OLIVINE FINE(47,3)\|MEDIATOR(46,8)\|MEASURING SENSOR(44,6)\|UPDATED MODEL(44,1)\|VOLCANIC MINERAL(41,3)\|ECOLOGICAL HARM(36,2)\|INGESTION(36,1)\|OLIVINE PARTICLE(35,6)\|OLIVINE MINERAL FINE(35,3)\|ECOLOGICAL CONDITION(35,1)\|FINE GRAIN(35,1)\|REACTION FLUX(32,3)\|INCREASE CO2 UPTAKE(31,1)\|OPERATING PARAMETER(31,1)\|OLIVINE SAND(30,20)\|COASTAL ENVIRONMENT(30,2)\|AQUATIC ENVIRONMENT(30,1)\|CARBON SEQUESTRATION(29,4)\|CO2 CAPTURE(28,10)\|PELLET(27,7)\|DISPERSION(27,1)\|INHALATION(27,1)\|LABOR INTENSIVE(27,1)\|CRUSHING(25,1)\|EFFLUENT(25,1)\|REACTIVITY(25,1)\|HEALTH HAZARD(24,1)\|MARINE LANDFILL CAP(23,6)\|OLIVINE DISSOLUTION KINETICS(23,3)\|COUNTERACTING OCEAN ACIDIFICATION COBENEFIT(23,1)\|BIOREACTOR(22,17)\|ACCELERATION(22,2)\|NATURAL CARBON REMOVAL(22,2)\|EQUIVALENTLY SIZED SOLID(21,2)\|COASTAL ENGINEERING(20,6)\|COASTLINE(20,5)\|INORGANIC FINE(20,3)\|REGULATION(20,2)\|MINERAL DUST(20,1)\|OLIVINE ENHANCING MATERIAL PROPERTY(20,1)\|TURBIDITY(19,4)\|MICROBIAL(19,1)\|TRANSPORTATION(18,5)\|INTERNAL POROSITY(18,2)\|CALCULATING ALKALINITY FLUX(17,3)\|COASTAL NOURISHMENT PROJECT(17,2)\|FUSION(16,2)\|MARINE ENVIRONMENT(16,2)\|SPLIT HULLED HOPPER BARGE(16,2)\|REMOVING CARBON(15,12)\|MINERAL(15,5)\|ENHANCED WEATHERING(15,4)\|PERMEABILITY(15,4)\|DREDGED SEDIMENT(15,3)\|BENTHIC INVERTEBRATE MEIOFAUNA(15,2)\|MARINE PHOTOSYNTHETIC MICROALGAE(15,1)\|OCEAN ACIDIFICATION MITIGATION(15,1)\|MICROBIAL BIOMASS(14,3)\|OCEAN ALKALINITY(14,3)\|OLIVINE DISSOLUTION BIOGEOCHEMICAL MODEL(14,1)\|SEA ACIDIFICATION COUNTERACTION(14,1)\|ROCK(13,11)\|CLAY MINERALOGY(13,2)\|CLAY SIMULTANEOUS PRECIPITATION(13,2)\|NONREACTIVE FEEDSTOCK(13,2)\|OCEAN DEACIDIFICATION(13,2)\|OLIVINE DISSOLUTION OPTIMIZATION(13,1)\|COASTAL CARBON CAPTURE(12,8)\|ACCELERATE OLIVINE(12,2)\|CR BIOACCUMULATION(12,2)\|HOPPER BARGE HULL(12,2)\|OLIVINE TRACER(12,2)\|ENGINEERED CARBON NEGATIVE MATERIAL(12,1)\|ENHANCING MATERIAL PROPERTY(12,1)\|TEMPORAL HETEROGENEITY EVALUATION(12,1)\|SHRINKING CORE MODEL(11,7)\|LARGE AGGREGATE(11,2)\|MICROBIAL PRODUCT(10,6)\|BIOMASS GENERATION(10,3)\|BEACH NOURISHMENT PROJECT(10,2)\|CALCULATING CO2 SEQUESTRATION(10,2)\|INTAKE SEAWATER(10,2)\|NI SPECIATION(10,2)\|OLIVINE REACTOR(10,2)\|PARTY ENTITY(10,2)\|PORE OVERVIEW(10,2)\|TOXIC POLLUTANT(10,2)\|BIOGENIC CALCIFICATION(10,1)\|CALCIFYING ORGANISM GROWTH(10,1)\|MARSH RESTORATION PROJECT(10,1)\|NEARBY COASTAL SHELF SEA(10,1)\|PHOTOSYNTHESIZING ALGAE(10,1)\|POREWATER GEOCHEMISTRY(10,1)\|SPATIOTEMPORAL HETEROGENEITY(10,1)\|SUCTION HOPPER DREDGE(10,1)\|SENSOR READING(9,5)\|CLAY FORMATION(9,4)\|CO2 TON(9,2)\|CLEAN UPLAND SAND(9,1)\|COASTAL COMMUNITY(9,1)\|FORSTERITE OLIVINE REACTION(9,1)\|FORSTERITE TON(9,1)\|ISOCAPNIC QUOTIENT(9,1)\|MARINE FOOD WEB CORNERSTONE(9,1)\|MITIGATING COASTAL EROSION(9,1)\|NET SILICATE DISSOLUTION(9,1)\|OCEAN ALKALINIZATION(9,1)\|OLIVINE ENHANCED DISSOLUTION(9,1)\|OLIVINE REDISTRIBUTION(9,1)\|OLIVINE SLOW DISSOLUTION(9,1)\|OLIVINE TRACKING(9,1)\|TURBIDITY PREDEPLOYMENT REDUCTION(9,1)\|ULTRAMAFIC INORGANIC MINERAL(9,1)\|SALINITY(8,5)\|GREEN HYDROGEN(8,4)\|MINERAL PROCESSING(8,3)\|TEMPORAL FACTOR(8,3)\|WEATHERING PRODUCT FORMATION(8,3)\|DEPLOYMENT SITE(8,2)\|DIATOM GROWTH(8,2)\|OLIVINE DISTRIBUTION(8,2)\|REGULAR CAP SAND(8,2)\|REGULATORY REQUIREMENT(8,2)\|SEAWATER AGE(8,2)\|WEATHERING(8,2)\|ALKALINITY EXPORT(8,1)\|ALKALINITY PROFILE NUMERIC SIMULATION(8,1)\|ALLOCHTHONOUS SAND(8,1)\|ANAEROBIC DIGESTION(8,1)\|ANAEROBIC RESPIRATION(8,1)\|APPLE IPHONE(8,1)\|ARTIFICIAL WEATHERING(8,1)\|ATTRIBUTE ENGINEERING(8,1)\|AUGMENT SEDIMENT(8,1)\|BEACH SEDIMENT(8,1)\|BENTHIC FLUX MEASUREMENT(8,1)\|CALCIFYING ORGANISM ABILITY(8,1)\|CALCULATING CO2 CAPTURE(8,1)\|CLAY PRECIPITATION(8,1)\|CRUSHED SANDSTONE(8,1)\|DIATOM ABUNDANCE(8,1)\|DISSOLUTION SIMULATION(8,1)\|EXTRACTING OLIVINE(8,1)\|GLOBAL LOGISTICS(8,1)\|GREEN VOLCANIC SILICATE MINERAL(8,1)\|HOPPER DREDGING(8,1)\|HYDROLOGIC SLURRY(8,1)\|INVOLUNTARY RESTRICTION(8,1)\|MARINE ECOSYSTEM HEALTH(8,1)\|MARITIME ASSET(8,1)\|MEASURING ALKALINITY FLUX(8,1)\|MITIGATE COASTAL EROSION(8,1)\|OLIVINE ABUNDANCE(8,1)\|OLIVINE DISSOLUTION ENVIRONMENT(8,1)\|REGIONAL OLIVINE DISSOLUTION RATE(8,1)\|SAND ENGINEERING REQUIREMENT(8,1)\|SEDIMENT DESTINATION(8,1)\|SUSTAINED MICROBIAL GROWTH(8,1)\|SUSTAINED SIDEROPHORE PRODUCTION(8,1)\|GRAIN SIZE(7,23)\|WAVE ENERGY(7,9)\|PLOT(7,7)\|COASTAL ENHANCED WEATHERING(7,5)\|BINDING AGENT(7,4)\|FLUID COMMUNICATION(7,4)\|MG2SIO(7,4)\|PHYSICAL COMPRESSION(7,2)\|PRIOR WORK(7,2)\|AGGREGATING RAW(7,1)\|ALK MOLE OLIVINE(7,1)\|ALKALINE SEAWATER(7,1)\|ALKALINITY CONSUMPTION(7,1)\|ARTIFICIALLY CREATED MINERAL(7,1)\|ATMOSPHERIC PCO(7,1)\|BENTHIC FLUX CHAMBER(7,1)\|BIOMASS SUSPENDED OLIVINE(7,1)\|CARBON CREDIT SALE VERIFICATION(7,1)\|CRUSHED LIMESTONE(7,1)\|DISSOLUTION BEHAVIOR(7,1)\|DISSOLVING OLIVINE(7,1)\|DREDGING MODIFICATION(7,1)\|EXTRACT OLIVINE(7,1)\|FLUX ACCURATE CALCULATION(7,1)\|INERT SAND(7,1)\|LADLE SLAG(7,1)\|LANDLINE NETWORK(7,1)\|MESOCOSM EXPERIMENT(7,1)\|METEOROLOGY IMPACT(7,1)\|MINERAL OLIVINE(7,1)\|NATIVE BEACH SAND(7,1)\|NATIVE SAND COLOR(7,1)\|NATURALLY CAPTURED CO2(7,1)\|NATURALLY OCCURRING NATIVE SEDIMENT(7,1)\|NATURALLY OCCURRING VOLCANIC MINERAL(7,1)\|NET CO2 FLUX(7,1)\|NONREACTIVE SEDIMENT COMPONENT(7,1)\|NONTOXIC CLAY(7,1)\|OCEAN ACIDITY(7,1)\|OCEAN SEDIMENT(7,1)\|OLIVINE DISSOLUTION RATE STUDY(7,1)\|OLIVINE FRACTION(7,1)\|OLIVINE MINERAL DISSOLUTION RATE(7,1)\|OLIVINE ROCK(7,1)\|OLIVINE TRANSPORT(7,1)\|OVERLYING SEAWATER(7,1)\|PERFECT SPHERE(7,1)\|POREWATER CHEMISTRY(7,1)\|PRECISE TIMESCALE(7,1)\|SAMSUNG TAB(7,1)\|SEA CO2 FLUX(7,1)\|SEAWATER CARBONATE(7,1)\|SEDIMENT HOPPER(7,1)\|SPARSE OBSERVATION(7,1)\|STABILIZING EARTH ATMOSPHERIC CO2(7,1)\|STRAIN OPTIMIZATION(7,1)\|COMPONENT REACTION(6,3)\|MACHINE EXECUTABLE CODE(6,3)\|PORE WATER PROFILE(6,3)\|PORTAL(6,3)\|PREDICTED RATE(6,3)\|ATMOSPHERIC CO2 UPTAKE(6,2)\|CIRCUM NEUTRAL PH(6,2)\|CO2 CONSUMPTION(6,2)\|COASTAL ECOSYSTEM(6,2)\|ECOLOGICAL RESPONSE(6,2)\|GAS CO2 FLUX(6,2)\|MAGNESIUM RELEASE(6,2)\|MICROMOL(6,2)\|MICROORGANISM(6,2)\|PARTICLE DISTRIBUTION(6,2)\|PHOTOSYNTHESIS(6,2)\|PROJECT SITE(6,2)\|WATER OXYGEN(6,2)\|ABSORB CO2(6,1)\|ACCURATE SIMULATION(6,1)\|ALKALINITY GENERATION(6,1)\|ALKALINITY MEASUREMENT(6,1)\|ALKALINITY SENSOR(6,1)\|ANALYTICAL MEASUREMENT(6,1)\|ATMOSPHERIC CO2 GIGATON(6,1)\|BEACH NOURISHMENT CYCLE(6,1)\|BIG FLUX(6,1)\|BIOMASS GROWTH(6,1)\|BLAST FURNACE SLAG(6,1)\|BOLSTERING LOCAL ECONOMY(6,1)\|CAPSIZING RISK(6,1)\|CARBON CREDIT VERIFIER(6,1)\|CARBONATE BEACH SAND(6,1)\|CARBONATE PRECIPITATION DISSOLUTION(6,1)\|COARSE PARTICLE(6,1)\|COASTAL ENGINEERING PROJECT(6,1)\|COMPUTER TANGIBLE MEMORY(6,1)\|CTDO SENSOR(6,1)\|CUSTOM STRAIN(6,1)\|DIURNAL FACTOR(6,1)\|DREDGING OPERATOR(6,1)\|ECOLOGICAL BENEFIT(6,1)\|ENHANCE OLIVINE(6,1)\|ENHANCED COASTAL EROSION(6,1)\|ENHANCING DISSOLUTION(6,1)\|EXCESS CO2 EMISSION(6,1)\|FE AVAILABILITY(6,1)\|FISHERY YIELD(6,1)\|GROUND OLIVINE(6,1)\|HUMAN CO2 EMISSION(6,1)\|IRON OXIDE(6,1)\|LEVER AGING NATURAL(6,1)\|MAGNESIUM RICH(6,1)\|MANAGEMENT SERVER(6,1)\|MARITIME EMISSIONS REDUCTION(6,1)\|MICROBIALLY MEDIATED TREATMENT(6,1)\|MINERAL REACTION(6,1)\|MONITOR OLIVINE(6,1)\|NATURAL SEAWATER(6,1)\|NET CAPTURE(6,1)\|OBJECTIVE CRITERIA(6,1)\|OLIVINE(6,1)\|OLIVINE DISSOLUTION SIGNAL(6,1)\|OLIVINE DISSOLUTION TEMPERATURE(6,1)\|OLIVINE GRAIN MOVEMENT(6,1)\|OLIVINE SPREADING LAYER(6,1)\|PROCESSED OLIVINE(6,1)\|PROTEINACEOUS COMPOUND(6,1)\|QUASI STEADY EQUILIBRIUM(6,1)\|RAW OLIVINE(6,1)\|RECIRCULATION LOOP(6,1)\|REVELLE FACTOR(6,1)\|SEAWATER RETURN(6,1)\|SEDIMENT MOTION(6,1)\|SEDIMENT TRANSPORT MODEL(6,1)\|SEDIMENT WATER ALKALINITY FLUX(6,1)\|SHALLOW SLOPE(6,1)\|SIDEROPHORE PRODUCTION YIELD(6,1)\|SILICATE BEACH SAND(6,1)\|SMALL OLIVINE GRAIN ENCAPSULATION(6,1)\|SOLUBLE BICARBONATE ION(6,1)\|STATIC DISSOLUTION(6,1)\|SULFIDE OXIDATION(6,1)\|TANGIBLE TRANSMISSION MEDIA(6,1)\|TARGET BEACH(6,1)\|WHITE OLIVINE(6,1)\|WIRED LINK(6,1)\|CPU(5,9)\|CO2 REACTIVE COMPONENT(5,5)\|SHIPPING(5,4)\|CORAL(5,3)\|SEAWATER PH(5,3)\|ALKALINITY FUNCTION(5,2)\|ATMOSPHERIC CARBON DIOXIDE(5,2)\|BASALT(5,2)\|BRUCITE(5,2)\|CARBON DIOXIDE EMISSION(5,2)\|CARBON NEGATIVE MATERIAL(5,2)\|CARBONATE PHASE(5,2)\|CHRYSOTILE(5,2)\|COMMUNICATION INTERFACE(5,2)\|EXTRANET(5,2)\|H4SIO4(5,2)\|INTRANET(5,2)\|ISOTOPIC TRACER(5,2)\|NATURALLY OCCURRING MINERAL(5,2)\|NUTRIENT(5,2)\|OLIVINE BREAKDOWN(5,2)\|REACTION TRANSPORT MODELING(5,2)\|SHOW DISSOLUTION(5,2)\|THRIVE(5,2)\|COMPUTER PROCESSOR(4,5)\|FLUORESCENT DYE(4,3)\|H2CO(4,3)\|MINING(4,3)\|QUARTZ(4,3)\|SHELL(4,3)\|SILICIC ACID(4,3)\|SPECTRAL PROPERTY(4,3)\|TEXTURE(4,3)\|TIDE(4,3)\|CLIENT(4,2)\|COASTAL PROTECTION(4,2)\|INTERNAL CHAMBER(4,2)\|ABUNDANT ION(4,1)\|ACCELERATE NATURAL CHEMICAL WEATHERING(4,1)\|AQUEOUS CO2 REMOVAL(4,1)\|BASELINE SITE(4,1)\|BICARBONATE PRODUCTION(4,1)\|BULK CARRIER DEPLOYMENT(4,1)\|BYPRODUCT(4,1)\|CAPTURE CO2(4,1)\|CARBON CAPTURE QUANTIFICATION(4,1)\|CARBON NEGATIVE SAND DISSOLUTION(4,1)\|CARBON REMOVAL VERIFICATION(4,1)\|CARBONATE PARAMETER(4,1)\|CARBONATE PRECIPITATION RATE(4,1)\|CLIMATE CHANGE MITIGATION LOCALE(4,1)\|COSTAL CARBON CAPTURE(4,1)\|DAMAGED AREA REGENERATION(4,1)\|DEPICTION(4,1)\|DIAGENESIS(4,1)\|DISSOLUTION MEASUREMENT(4,1)\|DISSOLUTION REACTION(4,1)\|DUAL BENEFIT(4,1)\|EXPOSED VOLCANIC ROCK(4,1)\|FINE FRACTION PARTICLE(4,1)\|FULL CARBONATE CHEMISTRY(4,1)\|GLOBAL MODEL(4,1)\|GLOBAL SCALE(4,1)\|GROUND NATURAL(4,1)\|INERT NATIVE(4,1)\|INORGANIC COATING(4,1)\|INORGANIC PARTICLE(4,1)\|INSOLUBLE IRON(4,1)\|LAND CONSTRUCTION(4,1)\|LARGE EFFECTIVE GRAIN SIZE(4,1)\|LIQUEFACTION REDUCTION(4,1)\|LIQUID ALKALINITY(4,1)\|MACHINE EXECUTABLE INSTRUCTION(4,1)\|MAGNESIUM ION(4,1)\|MEASURING TURBULENT ENERGY DISSIPATION(4,1)\|NATURAL BEACH SAND(4,1)\|NATURALLY OCCURRING OLIVINE(4,1)\|NATURALLY OCCURRING ROCK SEDIMENT(4,1)\|NEARBY COASTAL AREA(4,1)\|NITRATE SENSOR(4,1)\|NONTRANSITORY STORAGE(4,1)\|OCEAN REGION(4,1)\|OLIVINE CARBON CAPTURE REACTION(4,1)\|OLIVINE PROCESSING(4,1)\|OLIVINE THICK LAYER(4,1)\|OLIVINE VOLUME(4,1)\|REACTION NUMBER(4,1)\|REGULATORY PERMIT(4,1)\|SEAWATER MEDIUM(4,1)\|SEQUESTERING CARBON(4,1)\|SHALLOW MARINE ENVIRONMENT(4,1)\|SILICATE SENSOR(4,1)\|SIMULATION MODEL(4,1)\|SIMULTANEOUS BENEFIT(4,1)\|SOLUBLE MINERAL(4,1)\|SPECIALIZED SENSOR(4,1)\|STEEL FURNACE SLAG(4,1)\|SUBTROPICAL REGION(4,1)\|THERMODYNAMICS(4,1)\|TOTAL ALKALINITY SIMULTANEOUS MEASUREMENT(4,1)\|TRACK AIR SEAWATER(4,1)\|UNTRANSFORMED VOLUME(4,1)\|WIRELESS LINK(4,1)\|ACADEMIC(3,1)\|ACCEPTANCE(3,1)\|ACCOUNTING(3,1)\|AIR SEA CO2 EXCHANGE(3,1)\|AIR SEA EQUILIBRATION(3,1)\|ALKALINIZED SEAWATER ADDITION(3,1)\|ANDROID ENABLED(3,1)\|AQUACULTURE(3,1)\|ARAGONITE(3,1)\|ATMOSPHERIC GREENHOUSE GAS EMISSION(3,1)\|BIOLOGICAL ORGANISM(3,1)\|BIOTITE(3,1)\|BIOTURBATION(3,1)\|BLACKBERRY(3,1)\|CALCITE(3,1)\|CANDIDATE LOCATION(3,1)\|CARBON DIOXIDE CAPTURE(3,1)\|CARBON DIOXIDE IMPACT(3,1)\|CARBON DIOXIDE MOL(3,1)\|CARBON DISSOLUTION(3,1)\|CARBON NEGATIVE BATCH(3,1)\|CARBON REMOVAL PROJECT(3,1)\|CARBON REMOVING CAP BLEND(3,1)\|CELLULAR PROTEIN KEY COMPONENT(3,1)\|CHLORITE(3,1)\|CHLOROPHYL(3,1)\|CLIMATE CHANGE IMPACT(3,1)\|CO2 ABSORPTION RATE(3,1)\|CO2 OLIVINE RATIO(3,1)\|CO2 REACTIVE MINERAL COMPONENT(3,1)\|COASTAL ENGINEERING PRODUCT(3,1)\|COHESION(3,1)\|COLLISION(3,1)\|COMMUNICATION BUS(3,1)\|COMPUTER EXECUTABLE CODE(3,1)\|CONDUCTING CARBON NEUTRAL(3,1)\|CONSTRUCTION DEBRIS(3,1)\|CULTURING CONDITION(3,1)\|CUTTERHEAD DREDGING OPERATION(3,1)\|CYTOCHIP(3,1)\|DATABASE(3,1)\|DECADE(3,1)\|DEPTH MEASUREMENT(3,1)\|DISCRETE LOCATION(3,1)\|	(EP4166641)\|1. A system for processing olivine, comprising:\|a reactor for accelerating olivine weathering, wherein the reactor comprises one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate said olivine weathering.\|2. The system of claim 1, wherein the reactor is configured to adjust one or more operational parameters for processing olivine based on one or more sensors configured to measure carbon capture facilitated by said olivine weathering.\|3. The system of claim 1 or 2, wherein the olivine comprises pelletized olivine aggregates formed from olivine fines.\|4. The system of claim 3, wherein the olivine is prepared using [1] use of a binding agent, [2] via encapsulation of the olivine in one or more select materials or [3] via thermal fusion or physical compression of smaller olivine grains into larger aggregates.\|5. The system of claim 3 or 4, wherein the pellets are designed to either [i] remain substantially intact while maintaining improved surface area via internal porosity and permeability or [ii] degrade in a controlled fashion to release fine olivine fines to the environment in a prolonged controlled fashion.\|6. The system of any one of claims 3 to 5, wherein the preparation of the pellets allows olivine dissolution to occur substantially faster than would occur for equivalently sized solid pure olivine grains, improving the process of carbon capture, while minimizing the aesthetic, health, and ecological harm and challenges posed by working with and utilizing olivine mineral fines.\|7. A method, comprising:\| (a) generating one or more models for determining or predicting olivine dissolution, carbon sequestration, or one or more reaction fluxes associated with a dissolution of olivine in a target environment;\| (b) obtaining one or more sensor measurements at the target environment;\| (c) validating and/or updating the one or more models based on the one or more sensor measurements; and\| (d) using the one or more validated and/or updated models to determine or predict (i) olivine dissolution, (ii) carbon sequestration, and (iii) the one or more reaction fluxes in the target environment.\|8. The method of claim 7, wherein the target environment comprises a coastal or aquatic environment.\|9. The method of claim 7 or 8, further comprising providing olivine to the target environment.\|10. The method of claim 9, wherein the olivine is provided as part of a mixture comprising (i) the olivine and (ii) local beach sand at the target environment.	(EP4166641)\|CROSS REFERENCE\|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/256,986 filed on October 18, 2021, U.S. Provisional Patent Application No. 63/281,575 filed on November 19, 2021, and U.S. Provisional Patent Application No. 63/298,412 filed on January 11, 2022, each of which is incorporated herein by reference in its entirety for all purposes.\|BACKGROUND\|[0002] Enhanced weathering or accelerated weathering may be used to remove atmospheric carbon dioxide by leveraging natural or artificially created minerals that can absorb and transform carbon dioxide into other substances through chemical reactions that may occur in the presence of water (e.g., in the form of rain, groundwater or seawater).\|SUMMARY\|[0003] The present invention relates to a system for processing olivine. More specifically, the present invention relates to a system for processing olivine wherein the system comprises a reactor for accelerating olivine weathering, more particularly, the reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering. Enhanced weathering may be used in marine environments to increase ocean alkalinity and atmospheric CO2 uptake. In some cases, enhanced weather may involve adding processed minerals directly to the ocean or dumping the processed minerals on beaches where wave action can disperse the processed minerals into the target marine environment. Enhanced weathering may be used to reduce CO2 levels in the atmosphere while also counteracting ocean acidification.\|[0004] Recognized herein are various limitations with current weathering methods, which may (i) involve long lead times and labor intensive procedures, (ii) impact ecological conditions (e.g., increasing water turbidity), and (iii) handling/processing of minerals that can pose additional ecological and health hazards via the possible ingestion, contact, or inhalation of fine grain of olivine mineral dust.\|[0005] The present application relates generally to using olivine to achieve enhanced weathering and increase CO2 uptake on accelerated timescales. In one aspect, the present disclosure provides systems and methods for accelerating weathering. In another aspect, the present disclosure provides a bioreactor configured to accelerate dissolution of olivine for weathering applications. In a further aspect, the present disclosure provides systems and methods for enhancing material properties of olivine. For example, the present disclosure provides a way to optimize the surface area effect of fine olivine grains by utilizing a binding process to bind or encapsulate the olivine fines into pellets of a larger effective grain size which can be more safely handled and distributed in the environment. The ability to tailor the design of pellets composed of olivine mineral fines by using different binding agents or encapsulation processes provides the ability to tailor and control the porosity, permeability, and degradation characteristics of the olivine-containing pellets, controlling their dissolution behavior in the environment. The systems and methods disclosed herein may enable efficient processing and deployment of olivine for purposes of CO2 capture in marine environments.\|[0006] In some embodiments, pelletized olivine aggregates formed from olivine fines may be prepared through a number of processes disclosed herein including [1] the use of a binding agent (such as but not limited to clay, polysaccharides, proteinaceous compounds, resin, plastic, glass, etc.) [2] via encapsulation of smaller olivine grains with said binding agent or other similar materials or [3] via the thermal fusion or physical compression of smaller olivine grains into larger aggregates.\|[0007] In some embodiments, the pellets may be designed to either [4] remain substantially intact while maintaining improved surface area via internal porosity and permeability or [5] degrade in a controlled fashion to release fine olivine fines to the environment in a prolonged controlled fashion. In some cases, [6] the preparation of such pellets may allow olivine dissolution to occur substantially faster than would occur for equivalently sized solid pure olivine grains, thereby improving the process of carbon capture while minimizing the aesthetic, health, and ecological harm and challenges posed by working with and utilizing olivine mineral fines.\|[0008] Another aspect of the present disclosure provides a non-transitory computer readable medium comprising machine executable code that, upon execution by one or more computer processors, implements any of the methods above or elsewhere herein.\|[0009] Another aspect of the present disclosure provides a system comprising one or more computer processors and computer memory coupled thereto. The computer memory comprises machine executable code that, upon execution by the one or more computer processors, implements any of the methods above or elsewhere herein.\|[0010] Additional aspects and advantages of the present disclosure will become readily apparent to those skilled in this art from the following detailed description, wherein only illustrative embodiments of the present disclosure are shown and described. As will be realized, the present disclosure is capable of other and different embodiments, and its several details are capable of modifications in various obvious respects, all without departing from the disclosure. Accordingly, the drawings and description are to be regarded as illustrative in nature, and not as restrictive.\|INCORPORATION BY REFERENCE\|[0011] All publications, patents, and patent applications mentioned in this specification are herein incorporated by reference to the same extent as if each individual publication, patent, or patent application was specifically and individually indicated to be incorporated by reference. To the extent publications and patents or patent applications incorporated by reference contradict the disclosure contained in the specification, the specification is intended to supersede and/or take precedence over any such contradictory material.\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0012] The novel features of the invention are set forth with particularity in the appended claims. A better understanding of the features and advantages of the present invention will be obtained by reference to the following detailed description that sets forth illustrative embodiments, in which the principles of the invention are utilized, and the accompanying drawings (also "Figure" and "FIG." herein), of which:\| FIG. 1 schematically illustrates the long-term carbonate-silicate cycle, in accordance with some embodiments.\| FIG. 2 schematically illustrates the chemical processes by which olivine can be used to capture and sequester CO2, in accordance with some embodiments.\| FIG. 3 schematically illustrates the chemical reactions that enable CO2 capture and sequestration using olivine, in accordance with some embodiments.\| FIG. 4 schematically illustrates olivine and mixtures of sand and olivine, in accordance with some embodiments.\| FIG. 5 schematically illustrates one exemplary method for using olivine to remove atmospheric CO2 and increase ocean alkalinity, in accordance with some embodiments.\| FIG. 6 schematically illustrates the use of wave energy to cause sand grains and/or olivine grains to collide and break into smaller pieces, thereby facilitating the dissolution of olivine, in accordance with some embodiments.\| FIG. 7 schematically illustrates an example of how the oceans can be used for natural carbon storage, in accordance with some embodiments.\| FIG. 8 schematically illustrates an example of a bioreactor, in accordance with some embodiments.\| FIG. 9 schematically illustrates an example of a system for deploying olivine for coastal nourishment, in accordance with some embodiments.\| FIG. 10 schematically illustrates a computer system that is programmed or otherwise configured to implement methods provided herein.\| FIG. 11 schematically illustrates an exemplary reactor configured to intake seawater that may be mixed with olivine and microbial biomass to generate alkalinity.\| FIG. 12 schematically illustrates an exemplary protocol for measuring, recording, and verifying (MRV) carbon removal, in accordance with some embodiments.\| FIGs. 13 - 14 schematically illustrate a chemical reaction by which coastal carbon capture occurs when olivine is introduced to a target site, in accordance with some embodiments.\| FIGs. 15 - 20 schematically illustrate an environment in which olivine can be introduced for costal carbon capture, in accordance with some embodiments.\| FIGs. 21A and 21B schematically illustrates a plot of concentration of an alkaline material in a flux chamber as a function of time, in accordance with some embodiments.\| FIG. 22 schematically illustrates an overview of the porewater method, in accordance with some embodiments.\| FIG. 23 schematically illustrates a shrinking core model, in accordance with some embodiments.\| FIG. 24 schematically illustrates dissolution rates for olivine having various grain sizes, in accordance with some embodiments.\| FIG. 25 schematically illustrates an exemplary modeling approach for particle distribution, in accordance with some embodiments.\| FIG. 26 schematically illustrates dissolution rates for different mixtures of olivine having different mean grain sizes, in accordance with some embodiments.\| FIG. 27 schematically illustrates the impact of temperature and pH on olivine half-life, in accordance with some embodiments.\| FIG. 28 schematically illustrates examples of temporal factors and spatial factors that can vary for coastal ecosystems, in accordance with some embodiments.\| FIG. 29 schematically illustrates plots of the temporal heterogeneity of various characteristics for a target site, in accordance with some embodiments.\| FIGs. 30 - 32 schematically illustrate examples of factors to consider when calculating alkalinity fluxes, in accordance with some embodiments.\| FIG. 33 shows a summary of various approaches for measuring, recording, and verifying carbon capture and olivine dissolution at different scales of cost and complexity, in accordance with some embodiments.\| FIG. 34 schematically illustrates various reaction-transport modeling studies that may be used to simulate sediment porewater profiles, solid-phase chemistry, and benthic fluxes, in accordance with some embodiments.\| FIGs. 35 - 36 schematically illustrate various examples of sensors that can be used for measuring, recording, and verifying carbon capture and/or olivine dissolution, in accordance with some embodiments.\| FIGs. 37 - 38 schematically illustrate reactions that may occur when olivine sand is introduced to beaches, in accordance with some embodiments.\| FIG. 39 schematically illustrates an approach to calculating CO2 sequestration from alkalinity flux based on an expression of how water DIC storage changes as a function of increasing alkalinity, in accordance with some embodiments.\| FIG. 40 schematically illustrates a plot showing seawater age and the depth below sea water level of the Atlantic Ocean as a function of latitude (degrees North), in accordance with some embodiments.\| FIG. 41 schematically illustrates an exemplary coastal enhanced weathering (CEW) life cycle analysis, in accordance with some embodiments.\| FIG. 42 schematically illustrates an example of a carbon payback period that can be realized using the methods and systems disclosed herein, in accordance with some embodiments.\| FIG. 43 schematically illustrates various plots showing exemplary olivine dissolution kinetics for olivine particles having different grain sizes, in accordance with some embodiments.\| FIG. 44 schematically illustrates the effects of secondary carbonate precipitation on CO2 capture efficiency, in accordance with some embodiments.\| FIG. 45 schematically illustrates the effects of secondary clay formation on CO2 capture efficiency, in accordance with some embodiments.\|DETAILED DESCRIPTION\|[0013] While various embodiments of the invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. Numerous variations, changes, and substitutions may occur to those skilled in the art without departing from the invention. It should be understood that various alternatives to the embodiments of the invention described herein may be employed.\|[0014] Whenever the term "at least," "greater than," or "greater than or equal to" precedes the first numerical value in a series of two or more numerical values, the term "at least," "greater than" or "greater than or equal to" applies to each of the numerical values in that series of numerical values. For example, greater than or equal to 1, 2, or 3 is equivalent to greater than or equal to 1, greater than or equal to 2, or greater than or equal to 3.\|[0015] Whenever the term "no more than," "less than," or "less than or equal to" precedes the first numerical value in a series of two or more numerical values, the term "no more than," "less than," or "less than or equal to" applies to each of the numerical values in that series of numerical values. For example, less than or equal to 3, 2, or 1 is equivalent to less than or equal to 3, less than or equal to 2, or less than or equal to 1.\|[0016] The term "real time" or "real-time," as used interchangeably herein, generally refers to an event (e.g., an operation, a process, a method, a technique, a computation, a calculation, an analysis, a visualization, an optimization, etc.) that is performed using recently obtained (e.g., collected or received) data. In some cases, a real time event may be performed almost immediately or within a short enough time span, such as within at least 0.0001 millisecond (ms), 0.0005 ms, 0.001 ms, 0.005 ms, 0.01 ms, 0.05 ms, 0.1 ms, 0.5 ms, 1 ms, 5 ms, 0.01 seconds, 0.05 seconds, 0.1 seconds, 0.5 seconds, 1 second, or more. In some cases, a real time event may be performed almost immediately or within a short enough time span, such as within at most 1 second, 0.5 seconds, 0.1 seconds, 0.05 seconds, 0.01 seconds, 5 ms, 1 ms, 0.5 ms, 0.1 ms, 0.05 ms, 0.01 ms, 0.005 ms, 0.001 ms, 0.0005 ms, 0.0001 ms, or less.\|Overview\|[0017] To avoid the worst effects of climate change, we must rapidly remove billions of tons of CO2 from the atmosphere. There are currently no proven methods for doing so. There is an urgent need to identify carbon removal methods that are permanent, scalable, and economical.\|[0018] The earth's natural long-term carbonate-silicate cycle is how our planet has naturally captured CO2 over thousands of years. Over millennia, rain falling on exposed volcanic rock causes it to weather, which removes CO2 from the atmosphere as bicarbonate dissolved in water. This water flows to the oceans, where marine calcifying organisms incorporate the CO2 into their shells and skeletons. When they die, they form ocean sediment, ultimately becoming limestone.\|[0019] The systems and methods of the present disclosure enable the acceleration of Earth's natural carbon removal method of rock weathering, through the extraction, processing (e.g., crushing and/or grinding), and transportation of volcanic mineral olivine to coastlines for dispersal or distribution. In some embodiments, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process. In other embodiments, a bioreactor may be used to enhance and facilitate olivine dissolution. In either case, carbon dioxide may be removed from the atmosphere as the olivine breaks down.\|[0020] Coastal Carbon Capture, also known as Coastal Enhanced Weathering, can be categorized as a negative emission technology (NET) that removes and stores CO2 on long timescales (tens to hundreds of thousands of years). The process aims to accelerate the natural chemical weathering of the mineral olivine by spreading large amounts of ground olivine-containing rock onto coastlines or bioreactors positioned on or near such coastlines, where it can dissolve in seawater, thereby increasing the rate of CO2 absorption by the ocean.\|[0021] The present disclosure provides systems and methods for accelerating the Earth's natural carbon removal method of rock weathering, by extracting the volcanic mineral olivine, grinding it into sand, and deploying it on coastlines or in bioreactors located on said coastlines. There, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process. Carbon dioxide is removed from the atmosphere as the olivine breaks down.\|[0022] FIG. 1 illustrates the long-term carbonate-silicate cycle. The illustrated reaction is the foundation of the Long-Term Inorganic Carbon Cycle, which has been occurring for billions of years, stabilizing Earth's atmospheric CO2 concentrations, and in turn enabling life to thrive. In fact, carbon dioxide removal (CDR) through natural rock weathering consumes ~1 gigaton of CO2 every year. Natural CO2 removal through rock weathering may be achieved through the following steps:\| 1. Rain falls on volcanic rocks, slowly dissolving them.\| 2. Carbonic acid dissolved in the rainwater reacts with silicate from the rocks, shifting the equilibrium from carbonic acid to bicarbonate.\| 3. This bicarbonate flows to the ocean.\| 4. Marine organisms use this as calcium carbonate in their shells and skeletons; when they die this becomes limestone.\| 5. Limestone formed at the ocean floor eventually subducts, locking up the carbon for millions of years.\|[0023] FIG. 2 illustrates the chemical processes that are enabled by olivine to perform CO2 capture and sequestration. FIG. 3 illustrates the chemical reactions that enable CO2 capture and sequestration using olivine. As the olivine dissolves, its products are magnesium ions (the second most abundant ion in the ocean behind sodium), silicate (used by diatoms to build their skeletons) and dissolved carbon. Referring to FIG. 2 and FIG. 3, when olivine dissolves in water, it drives the illustrated reaction, thus increasing CO2 uptake, raising pH, and generating alkalinity. As a result, this process has the potential co-benefit of counteracting ocean acidification. Ocean acidification is the process by which increasing atmospheric CO2 dissolves in seawater, which reduces pH (increasing acidity) (upper reaction in diagram below). This reduces the ability of calcifying organisms like corals to grow and produce exoskeletons, or shells. As shown in FIG. 2 and FIG. 3, dissolving olivine in water sequesters hydrogen ions into dissolved silicate (H4SiO4), a molecule that can be used by diatoms, an important photosynthesizing algae that fixes carbon dioxide and forms the base of food web.\|[0024] Unfortunately, natural chemical weathering happens too slowly to balance human CO2 emissions and is already accounted for in Earth's present-day carbon budget. The systems and methods disclosed herein can be deployed and implemented to accelerate this natural process to remove at least a gigaton of atmospheric CO2 per year on a global scale.\|Accelerating a Natural Process\|[0025] Coastal Carbon Capture can be used to accelerate Earth's natural CO2 removal process. At current rates, the natural process of rock weathering through rainfall needs to be sped up by at least 100 times to absorb the CO2 emitted by human activity. Coastal Carbon Capture (CCC) can accelerate the process by using wave energy and/or bioreactors to break down olivine. The rock containing the olivine may be placed in high-energy coastal environments, where wave energy mechanically activates the rock, causing collisions which remove the silica coating and efficiently grind the olivine down. The olivine sand then dissolves in the water at a rate orders of magnitude faster than in the geological process.\|[0026] Coastal Carbon Capture may comprise the following steps:\| 1. Extract olivine and efficiently grind it. Olivine is a green volcanic silicate mineral. It is highly abundant and found near the surface all over the world. Olivine rocks can be efficiently crushed to sand and gravel grain sizes.\| 2. Transport olivine to a nearby coastal area. The olivine sand may be transported (e.g., by rail, ship, or truck) to a nearby coastal shelf sea. There, it may be spread in a thin layer.\| 3. Wave energy may accelerate CO2 removal. Wave energy and currents may further grind down the olivine. Grain-on-grain collisions can cause fine fraction particles (< 10 microns) to form, which then weather very rapidly. The olivine may consequently dissolve in the water rapidly, accelerating the reaction which removes CO2 from the ocean/atmosphere.\|[0027] FIG. 5 illustrates one exemplary method for using olivine to remove atmospheric CO2 and increase ocean alkalinity. As shown in FIG. 6, wave energy may cause sand grains and/or olivine grains to collide and break into smaller pieces, thereby facilitating the dissolution of olivine.\|Olivine\|[0028] Olivine is a common, naturally occurring volcanic mineral, with physical properties similar to quartz. Olivine may be 23% denser than quartz sand (1.43 tons/cy). Olivine sand is a clean upland sand that is 25% denser than silicate sand, and that can be artificially milled to match native grain size. Darker and lighter olivine sources allow for color matching to the native sand color.\|[0029] Olivine can be processed to yield fine olivine grains with increased surface area exposure, which can speed up dissolution and the CO2 capture process. The olivine dissolution and CO2 capture process can also be accelerated by (i) using reactive and soluble minerals, (ii) increasing an amount of surface area of the olivine grains that is exposed to a solvent (e.g., water or seawater), (iii) enhancing fluid-mineral interactions, and/or (iv) reducing or eliminating secondary mineral coatings or the formation of secondary weathering products (e.g., precipitation of secondary clays and carbonate phases).\|[0030] Once deployed on a beach, olivine can capture 20 times more carbon than is emitted in the mining, milling, shipping, and beach nourishment operation. 1 ton of olivine sand can capture up to 1.25 tons of carbon in ideal situations. Since it takes olivine several decades to weather, it will provide effective coastal protection during long-term beach nourishment cycles.\|[0031] One type of olivine may be white olivine, or Forsterite (Mg2SiO4). This is a magnesium rich form of olivine, known as Forsterite (Mg2SiO4). Weathering 1 ton of olivine can remove up to 1.25 tons of CO2 from the atmosphere.\|[0032] FIG. 4 illustrates olivine and mixtures of sand and olivine. In some cases, the olivine may be mixed with natural beach sand before the olivine is deployed at a target site. The mixture comprising the olivine may comprise at least about 5%, 10%, 15%, 20%, 25%, or 30% olivine by weight or volume. In some cases, the mixture may comprise more than 30% olivine by weight or volume. In some cases, the mixture may comprise less than 5% olivine by weight or volume. In some cases, the mixture may comprise between about 5% and about 30% olivine by weight or volume.\|[0033] Beneficial applications of olivine include, for example, Marsh Restoration, Coastal Engineering/Hazard Mitigation, and CO2 Capture. As described above, olivine sand can react with water and CO2. CO2 may dissolve in water to form carbonic acid. Olivine dissolution may consume the carbonic acid to yield soluble bicarbonate ion (baking soda). This can: Lower atmospheric CO2, Neutralize ocean acidification, and Support the growth of calcifying organisms (Corals, etc).\|[0034] In some cases, olivine sand may be provided to municipalities to augment the sediment used in beach nourishment projects. As the sand weathers, it captures carbon. The sand and its placement are paid for by carbon credits. Therefore, the greater the percentage of olivine sand mixed into the native sand, the cheaper the beach nourishment project. A 10% mix would mean a -10% decrease in sand cost. Through the use of olivine sand, beach nourishment can play a critical role in reversing climate change and ocean acidification if the right mix of native and olivine sand is used. At scale, over a billion tons of CO2 could be removed from the atmosphere every year.\|[0035] Using wave action to break down the olivine is critical to the life cycle. Past analyses have shown that grinding the olivine down to <100µm size is highly energy-intensive. However, grinding the olivine down to >300µm gravel requires far less energy. Using the natural, free energy of water movement to break the olivine down further reduces the milling and grinding energy to a small proportion of the total.\|[0036] Co-Benefits of the methods described herein include, for example: reduction in Ocean Acidification (OA). Ocean acidification has been shown to damage marine ecosystems. Olivine increases local pH levels, potentially mitigating the adverse effects of OA on marine ecosystems. This could potentially improve aquaculture and fishery yields, bolstering local economies at deployment sites as well as reversing damage to marine ecosystems. FIG. 7 illustrates an example of how the oceans can be used for natural carbon storage. Excess CO2 emissions may increase ocean acidity. The systems and methods of the present disclosure may be implemented to reduce acidity and help the oceans safely store more CO2 as bicarbonate.\|[0037] Co-Benefits of the methods described herein may also include, for example: support for diatom growth. Diatoms, marine photosynthetic microalgae, are a cornerstone of marine food webs and capture CO2 through photosynthesis, creating 40% of oxygen on Earth. Diatom abundance has decreased as CO2 has risen, partly due to decreasing concentrations of silicate in the ocean due to damming of rivers limiting sediment flow. Since olivine is primarily magnesium silicate, the increase in silicate concentrations from olivine dissolution may lead to diatom growth. Increases in diatoms would increase the health of marine ecosystems and support photosynthetic carbon capture. Other co-benefits can include, for example, supporting coastal communities facing enhanced coastal erosion and sea level rise by supplying a low-cost source of sediment (which may be paid for using carbon credits).\|Mechanics of Weathering\|[0038] In some cases, grain-on-grain collisions may rapidly break down the olivine. Olivine grains may be reduced in size due to mechanical activation. In some cases, the motion of the water in which the olivine is provided may cause surface abrasions. In some cases, the surface of the olivine grains may be mechanically activated to enable and/or enhance CO2 uptake and de-acidification.\|Sensors\|[0039] In some cases, one or more sensors may be used to track, monitor, and quantify olivine dissolution, CO2 uptake, and ocean de-acidification. The measurements obtained using the sensors may be used to adjust the preparation or processing of the olivine, the optimal properties of the olivine, the location in which the olivine is introduced, the rate at which the olivine is introduced, a method by which the olivine is distributed, or a configuration/form in which the olivine is distributed.\|[0040] In some cases, the one or more sensors may be used to monitor and track: Olivine Dissolution Rates (Porewater Geochemistry, Benthic Flux Measurements), Impacts on Water Chemistry, Ecological Response, Fate, Transport and Bioaccumulation of Cr and Ni, and/or Formation of Secondary Weathering Products (Chrysotile, Carbonates, Clays). In some cases, an isotopic tracer along with [Si] and [ALK] measurements may be used to track olivine dissolution and simultaneous precipitation of secondary clays and carbonate phases. The sensors may also be used to track olivine grains over time [ie physical tracking of olivine using dyes / tracers, etc.].\|Reaction-Transport Modeling\|[0041] In some cases, simulation models may be used to optimize the preparation or processing of the olivine, the properties of the olivine, the location in which the olivine is introduced, the rate at which the olivine is introduced, a method by which the olivine is distributed, or a configuration/form in which the olivine is distributed. The models may be configured to simulate sediment porewater profiles, Water column and Porewater Chemistry (e.g., pCO2, DIC, pH, DO, TA, Nutrients, Metals, DOC), solid-phase chemistry and benthic fluxes, Secondary Clay Mineralogy, and Cr and Ni speciation and cycling. In some cases, the models may be used for simulation of the effects of spreading layers of olivine sand of varying thicknesses on a target beach sediment with one or more known biological, chemical, or ecological properties or characteristics.\|[0042] In some cases, the models may be used simulate or predict Olivine Dissolution Rates, study the impacts of Temperature of Olivine Dissolution & Respiration, track impacts on seawater pH, track Air-Sea Water Gas CO2 Fluxes, monitor and evaluate fate and transport of Cr and Ni, assess the impacts on benthic invertebrates/meiofauna, track sediment characteristics (e.g., changes in mineralogy, formation of secondary carbonate/clays), monitor the impacts of Meteorology and Hydrology (e.g., temperature, wind speed/direction, precipitation, salinity, turbidity, current), or simulate Physical Sediment Transport and/or Olivine Redistribution.\|Method of Removing Atmospheric Carbon\|[0043] [1] In one aspect, the present disclosure provides a method for removing atmospheric carbon using olivine dissolution technologies. The method may be implemented using natural wave energy (i.e., in situ coastal enhanced weathering (CEW)) and/or applied energy (i.e., closed-system artificial weathering of olivine in a man-made reactor or a sand pit resulting from coastal nourishment projects or dredging).\|Bioreactor\|[0044] In another aspect, the present disclosure provides systems and methods to accelerate olivine dissolution reactions in a bioreactor. The bioreactor may comprise one or more internal chambers for housing or storing olivine for any amount of time. The bioreactor may comprise one or more openings or inlets for receiving olivine. The olivine may comprise pure olivine or a mixture of olivine and sand or other elements or materials. The olivine may be unprocessed. Alternatively, the olivine may be processed or pre-processed (e.g., by grinding).\|[0045] In some cases, the bioreactor may comprise one or more mechanical components for mechanical weathering of the olivine. The mechanical weather may cause grain-on-grain collisions that may rapidly break down the olivine. Olivine grains may be reduced in size due to mechanical activation. In some cases, the bioreactor may be in fluid communication with water. In some cases, the bioreactor may comprise an internal chamber for housing the water and/or the olivine. The motion of the water in which the olivine is introduced may cause surface abrasions. In some cases, the surface of the olivine grains may be mechanically activated to enable and/or enhance CO2 uptake and ocean de-acidification.\|[0046] In some cases, the mechanical components may comprise one or more gears or actuators for inducing a motion that cause mechanical weathering of the olivine. The motion may be a linear motion, or a rotational motion, or any combination thereof.\|[0047] In some cases, the bioreactor may comprise a chamber for housing one or more microbial products or other biological mediators and/or enzymatic accelerants that can help to further break down the olivine. The chamber housing the microbial products may be in fluid communication with (i) the chamber housing the olivine, (ii) the chamber that is in fluid communication with the ocean water, or both (i) and (ii).\|[0048] FIG. 8 schematically illustrates an example of a bioreactor 800. The bioreactor 800 may be configured to receive olivine, which olivine may or may not be pre-processed (e.g., by grinding or crushing). The olivine may be stored within a first chamber 810 of the bioreactor 800 for further processing. In some cases, the bioreactor 800 may comprise a second chamber 820 configured to house one or more microbial products or other biological mediators and/or enzymatic accelerants that can help to further break down the olivine. In some cases, the bioreactor 800 may comprise a third chamber 830. The third chamber 830 may comprise a reaction chamber in fluid communication with the first chamber 810 and the second chamber 820. The third chamber 830 may be used to break down the olivine using the microbial products or other biological mediators and/or enzymatic accelerants. Once broken down, the processed olivine may be provided to a target region external to the bioreactor 800 to facilitate CO2 capture and sequestration.\|Microbes\|[0049] [2] In another aspect, the present disclosure provides a method for enhanced dissolution of olivine through (1) microbial products or other biological mediators and (2) enzymatic accelerants. The method may comprise enhancing dissolution of olivine in an olivine reactor or sand pit resulting from coastal nourishment projects or dredging through: microbial products or other biological mediators; and enzymatic accelerants.\|[0050] In another aspect, the present disclosure provides systems and methods for olivine dissolution by microorganisms, biological organisms, and/or biological mechanisms. The dissolution of olivine in water may consume protons and increase alkalinity, thereby removing dissolved aqueous CO2. This aqueous CO2 removal may induce additional CO2 to be taken up from the atmosphere and subsequently converted to bicarbonate, carbonate, and/or solid-phase carbonate minerals, thereby sequestering carbon for long time periods [1]. Scaling and accelerating this process has the potential to mitigate climate change and ocean acidification.\|[0051] In some cases, the reactors disclosed herein may be designed to grow particular microbial strains in an aqueous medium in order to induce metabolic states that can accelerate olivine dissolution. In circum-neutral pH naturally oxygenated waters, ferric iron (Fe2+) contained within olivine may be rapidly oxidized to ferrous iron (Fe3+) by oxygen even in the absence of microbial activity [2]. This oxidized iron can form a surface layer of Fe-oxyhydroxides on the mineral surface of olivine which can shield portions of its total surface area from contact with solution [3]. These Fe-oxyhydroxide surface coatings can, in some cases, impede olivine dissolution [4].\|[0052] For the vast majority of organisms, Fe is a required nutrient and a key component of many cellular proteins. However, most Fe in naturally oxygenated waters at circum-neutral pH is insoluble and typically complexed to particles. Certain microorganisms can produce organic compounds known as siderophores to mobilize and acquire insoluble iron on mineral surfaces [2], which can concurrently increase olivine mineral dissolution rates [3]. However, the production of siderophores may be regulated by Fe availability to the cells. As more Fe is acquired by the cells (i.e. the less iron-limited they are), siderophore production may decrease, which may slow dissolution rates. Hence, in order to sustain and scale siderophore production over extended time periods in large reactors, numerous interacting factors may be optimized:\| 1. The most optimized biological strains (these may be identified through a series of experiments, and in some cases, custom strains may be generated either through directed evolution or genetic editing).\| 2. The optimal ratios of microbial to siderophore concentrations given certain growth conditions.\| 3. Olivine dissolution optimization as a function of particle size/surface area and flow rate from biomass generation.\| 4. Optimized long-term growth conditions for sustained siderophore production.\| 5. Optimized reactor design series including appropriate materials to avoid silicate and trace metal contamination.\| 6. Development of mathematical model to optimize siderophore production yield, biomass generation, and olivine dissolution.\| 7. Development of appropriate parameters to track to feed into the model.\| 8. Development of any treatment of seawater effluent prior to returning to the ocean.\| 9. Development of a model that calculates CO2 sequestration from the addition of alkalinized seawater to the local ocean region.\|System Design\|[0053] Referring to FIG. 11, the illustrated reactor may be configured to intake seawater that may be mixed with olivine and microbial biomass to generate alkalinity. Depending on the source, seawater may have to be pretreated prior to reacting with olivine. This reaction may also result in trace metals, microbial biomass, and other reaction products mixing in with the seawater medium. In order to sequester carbon at scale, this alkaline seawater may be returned to the ocean to induce atmospheric CO2 uptake. Importantly, the return of this seawater containing the certain constituents must meet local regulations. Another microbially-mediated treatment process that returns effluent to the environment may involve anaerobic digestion. This may be a good reference to understand regulations for effluent from microbial processes.\|[0054] In some cases, the reactor may comprise a first chamber for biomass generation (e.g., continuous, semi-continuous, membrane bioreactor), a second chamber for olivine dissolution (e.g., to optimize particle size and flow/recycle biomass), and a third chamber for biomass/suspended olivine separation (and for biomass return to the first chamber). In some cases, sea water based growth media may flow into and/or out of the first chamber. In some cases, CO2 from biomass growth may be provided to the second chamber. The second chamber may also receive biomass with siderophores from the first chamber. The second chamber may provide, in some cases, a recirculation loop for the biomass. The second chamber may be configured to provide the biomass without the siderophores to the third chamber. In some cases, the third chamber may be configured to return biomass to the first chamber. In some cases, the third chamber may be configured to provide the olivine and/or the biomass to seawater.\|[0055] The present disclosure effectively provides methods and designs for sustained microbial growth and siderophore production for olivine dissolution over long time periods. Current methods are unable to accelerate olivine dissolution with microbes for reaction volumes exceeding a few hundred milliliters, unlike the systems and methods disclosed herein. The presently disclosed systems and methods have been developed with the specific engineering and regulatory requirements needed to build large-scale, flow-through reactors with seawater that will then be returned to the local environment. The present disclosure effectively provides systems and methods for optimizing (1) strain selection for olivine dissolution, (2) grain size, (3) culturing conditions with natural seawater, and (4) the materials for the growth chamber.\|Optimizing Olivine\|[0056] [3] In another aspect, the present disclosure provides systems and methods for optimizing olivine for use in the field. Such optimization may comprise, for example, determining the optimal grain size distribution of olivine sand for use in carbon capture (covers combinations of grain size, color, blends, includes modeling grain size for specific sites); and physically and/or chemically processing the olivine (e.g., using machinery) to prepare one or more batches of carbon negative sand suitable for beach nourishment.\|Preparing Olivine\|[0057] [4] In another aspect, the present disclosure provides systems and methods for preparing olivine grains for optimal dissolution. The olivine grains may be part of a source material comprising olivine sand or a mixture comprising olivine sand and local sand.\|[0058] In some cases, the method may comprise crushing raw olivine to yield an optimal grain size and aggregating raw or crushed olivine into pellets. Such processing of the olivine may enhance dissolution of olivine, thereby accelerating the carbon capture process. In some cases, the method may further comprise selecting, milling, and/or matching olivine sand to native sediment for the purpose of coastal protection, beach nourishment and carbon capture.\|[0059] In another aspect, the present disclosure provides carbon-negative sand and processes for producing the same. The carbon-negative sand may comprise specially selected, prepared, and blended mineral particles which [1] are suitable to mitigate coastal erosion along coasts [2] react with carbon dioxide (CO2) and/or dissolved carbonic acid [H2CO3] to produce bicarbonate [HCO3-], [CO32-] ions, and/or solid-phase carbonate minerals [Ca, Mg]CO3, thus [3] simultaneously mitigating the impacts of climate change, ocean acidification, and coastal erosion.\|[0060] In order to be suitable for use in coastal erosion, beach nourishment, and marsh restoration projects, [4] manufactured carbon-negative sand and blends thereof should closely match the texture, grain size distribution, and color of native sediment. Thus, the processes for preparing carbon negative sand may be tailored such that the carbon-negative sand and blends thereof produce and achieve these specific pre-determined properties.\|[0061] In order to mitigate the impacts of carbon dioxide (ie. be "carbon negative"), [5] carbon negative sand may be manufactured from a mafic or ultramafic inorganic mineral or rock (typically naturally occurring olivine, basalt, serpentinite, brucite, wollastonite, or industrial-produced mineralequivalents such as slag). These minerals [6] may react with water and carbon dioxide and/or carbonic acid to produce bicarbonate ion as a reaction product, thereby decreasing the acidity of the surrounding fluid and converting the harmful carbon dioxide or carbonic acid into environmentally beneficial bicarbonate or carbonate ion. An example describing the reaction of forsterite olivine (Mg2SiO4) is provided below, although other minerals and rocks described in this disclosure result in equivalent reactions converting carbonic acid to bicarbonate ion:\| CO2 + H2O → H2CO3\| Mg2SiO4 + 4 H2CO3 → 2 Mg2+ + 4 HCO3- + H4SiO4\|[0062] In order to simultaneously achieve the engineering requirements of sand and sediment for coastal engineering, while preserving the chemical reactivity with carbon dioxide described above, [7] it may be necessary to prepare specially prepare the reactive mineral components and then blend these reactive components in specifically determined ratios with inert native or allochthonous sand and sediment to achieve the desired chemical, engineering, and aesthetic properties. This process is described in greater detail below:\|[0063] The process for preparing the CO2 - reactive component of carbon negative sand begins with a feedstock of mafic or ultramafic rocks, minerals, or their industrially produced equivalents. A list of potential feedstocks is provided in Table 1.\|[0064] Table 1. Potential feedstock materials for the production of the CO2 - reactive component of carbon negative sand.\|Naturally Occurring Rocks: Peridotite, Dunite, Harzburgite, Lherzolite, Basalt, Gabbro, Komatiite, SerpentineNaturally Occurring Minerals: Olivine, Forsterite, Fayalite, Enstatite, Pyroxene, Serpentine, BruciteIndustrial Byproducts: Blast-furnace Slag, Steel-furnace Slag, Basic-oxygen-furnace Slag, Electric-arc-furnace Slag, Ladle Slag.\|[0065] The preparation of the CO2 - reactive components of carbon negative sand may proceed via two critical steps:\| (1) The feedstock may be crushed and/or milled to increase the reactive surface area of the feedstock and provide fresh reactive surfaces for the reaction with carbon dioxide. Because the reaction occurs only on the surfaces of the grains and within microcracks created by the crushing/milling process, it is essential to increase the available reaction surface area to the maximum extent possible in order to maximize the material reactivity.\| (2) The crushed and milled material may then be size sorted using sieves, gravity separation, air classifiers, to provide a final product with a mean grain size and overall grain size distribution which meets the engineering specifications of the coastal engineering project. In some cases, this process may be designed to exclude excessive fine-grained material and/or coarser particles, to produce an intermediate grain-size material which closely matches the size distribution of the native sediment in the geographic region receiving the carbon negative sand. As an alternative to preparing batches of CO2 - reactive components individually, it is also possible to presort the material into various predetermined size ranges and then select and/or blend from these preclassified separates to achieve an overall blend suitable for use in a specific project.\|In most cases or all cases, the CO2 - reactive component may be further modified via mixing non-reactive sediment in order to achieve a combination of texture, color, and density, and engineering properties suitable for use in coastal engineering products. To achieve this, a third step may be required:\| (3) The CO2-reactive mineral component may be blended with one or more chemicallyinert sand and sediment materials to achieve a predetermined ratio providing the specified properties. A list of common non-reactive feedstocks is provided in Table 2. Blends consisting of 1-50% reactive component may be most common, but other variations of this invention, higher or lower fractions of the reactive component may be used.\|Table 2. Potential feedstock materials for the non-reactive component of carbon-negative sand.Naturally Occurring Native Sediment at the Project Site: May include native sand, silt, clay, organic matter and gravelNaturally Occurring Rocks/Sediment: Silicate Beach Sand, Carbonate Beach Sand, Dredged Sediment, Crushed Sandstone, Crushed Limestone, Carbonate OoidsNaturally Occurring Minerals: Quartz, Feldspar, Aragonite, Calcite, Garnet, Magnetite, Hematite, Limonite, Ilmenite, Smectite, Chlorite, Biotite, Muscovite, Rutile, Zircon and Monazite\|[0066] The goal of blending the reactive- and non-reactive sediment components is to achieve a final bulk product meeting various regulatory, aesthetic and engineering requires including color, texture, grain size, density, cohesion, hardness, etc. To realize a blended mixture between the reactive and non-reactive components of the carbon-negative sand mixture, the individual components may either be brought together in advance, or in alternate embodiments, separately conveyed or placed onto the project site in such a manner to realize an appropriate mixture over the duration of the project (ie. mixing between components occurs via the physical motion of sediment driven by conveyors, heavy equipment, and/or waves and tides).\|[0067] Although enhanced silicate weathering may be implemented in some instances, none of the prior work has [8] recognized and provided methods for the manufacture of engineered carbon-negative materials with specific suitable colors, grainsize, density, and reactivity required to meet specific regulatory, aesthetic, and engineering requirement for coastal engineering. Moreover, [9] prior work has completely neglected the engineering of these specific attributes in order to create safe and successful materials for coastal engineering applications. [10] No existing material used in present coastal engineering applications provides additional public and ecological benefits due to CO2 capture, alkalinity generation, and the mitigation of ocean acidification. Likewise, [11] no prior approaches have realized the simultaneous benefits derived from manufacturing carbon-negative materials which are suitable for coastal engineering, thus providing a dual benefit of mitigating coastal erosion and sea level rise.\|Carbon Credits\|[0068] [5] In another aspect, the present disclosure provides systems and methods for measuring, recording and verifying (MRV) carbon removal as well as ecological effects of olivine sand in carbon removal over large coastal areas. Such measurements, recording, and verification of carbon removal may be performed using one or more remote sensors, protocols for the use of such sensors (benthic flux chambers), and algorithms to interpret the data obtained and derived from the sensor readings. The presently disclosed systems may be used to prove the dissolution of olivine and the subsequent capture of CO2 based on the dissolution of the olivine. In some cases, the systems and methods disclosed herein may be implemented to predict dissolution (e.g., by utilizing one or more models for simulating or predicting olivine dissolution at a target site).\|[0069] The present disclosure also provides software configured to calculate CO2 consumption and to measure/record/verify carbon removal. The software may be configured to determine CO2 consumption and/or carbon removal based on one or more sensor readings and/or one or more input parameters. The one or more input parameters may relate to, for example, the physical or chemical properties of the olivine used, the ratio of olivine to sand, the location in which the olivine is distributed, an amount of olivine distributed to a target site, or the manner/configuration in which the olivine is distributed (e.g., method of distribution, form of distribution, or spatial characteristics of the distribution). In some cases, the sensor readings may comprise measurements of alkalinity, pCO2, pH, and/or water temperature.\|[0070] In one aspect, the present disclosure provides methods and protocols for measuring, recording, and verifying (MRV) carbon removal (e.g., by way of coastal carbon capture using olivine). Referring to FIG. 12, the protocols may be submitted to independent, third-party entities (e.g., academics, institutions, etc.) for validation. Once validated, the protocols may be implemented by an individual or an entity. Additional third-party entities may ensure and confirm compliance. The individuals or entities implementing the MRV protocols may then submit the third-party verified, compliant methodologies to a carbon credit verifier, and an offset or a credit may be issued on a registry for sale in domestic and/or international markets.\|[0071] FIGs. 13 - 14 and FIG. 37 show a reaction representing the chemical mechanism by which coastal carbon capture can occur when olivine is introduced to a target site (e.g., by adding olivine sand to beaches and mixing the olivine sand with the native beach sand). For every 1 mol of olivine (which olivine may comprise or exhibit any of the physical or chemical properties or compositions described herein), 4 mols of carbon dioxide may be consumed or captured, and 4 mols of an alkaline material (bicarbonate or HCO3-) may be generated.\|[0072] FIGs. 15 - 20 show an environment comprising a first layer comprising seawater and a second layer comprising sediment and pore water. The sediment and pore water may span a dimension of about 10 centimeters (cm) or about 4 inches (in). The reactions shown in and described in relation to FIGs. 13 - 14 and FIG. 37 may drive the capture of carbon dioxide (e.g., CO2 in the atmosphere or in the seawater) and the release of magnesium, bicarbonate, and silicic acid. The rate of the overall reaction may be determined based on the fluxes associated with CO2 capture and the subsequent release of magnesium, bicarbonate, and silicic acid.\|[0073] In some non-limiting embodiments, one or more stirrers may be used to facilitate the carbon capture process (e.g., by physically mixing the seawater containing olivine sediments with the medium comprising the carbon dioxide). The medium may comprise a liquid medium (e.g., seawater) or a gaseous medium (e.g., air comprising atmospheric carbon dioxide). In some non-limiting embodiments, one or more valves may be used to control and regulate an outflow of any products of the reaction (e.g., the magnesium, bicarbonate, and/or silicic acid).\|[0074] FIG. 21A illustrates a plot of a change in concentration of an alkaline material in a flux chamber as a function of time when the olivine-based carbon capture reactions of the present disclosure are used. The alkalinity of the medium in which the alkaline material is present may gradually increase over time. In some cases, the alkalinity may increase by a factor of 1.1 to 10 or more over a period of 1 to 10 days. As shown in FIG. 21B, the alkalinity flux with olivine increases more rapidly over time than the alkalinity flux at a control site in which olivine is not introduced. The alkalinity flux may correspond to the slope of the lines shown in these plots, and may have units of change in concentration of the alkaline material per unit time.\|[0075] FIG. 22 shows an overview of the porewater method for determining flux of an alkaline material that is produced. The porewater method may be based on Fick's first law of diffusion. The flux of the alkaline material may be determined based on a diffusion coefficient (representing area per unit time) and a dC/dZ value (representing a change in concentration or amount of substance per unit volume, as a function of position or dimensional length). With olivine present in porewater, a larger flux may be observed (steeper slope and bigger flux), whereas when olivine is not present, a smaller flux is observed (shallower slope and smaller flux).\|[0076] FIG. 23 shows a shrinking core model comprising a transformed volume and an untransformed volume of an exemplary olivine particle. The shrinking core model may be represented by X = 1 - [1 - R/(ρ∗d))∗t]^3, where X is the fraction of olivine reacted, R is a function of pH and temperature, p is molar density, d is starting diameter, and t represents time. One assumption for this model is that the particles are a perfect sphere.\|[0077] FIG. 24 shows dissolution rates for olivine having various grain sizes. The fraction of olivine reacted over time may increase more rapidly for olivine particles having smaller grain sizes. For example, for olivine with a 30 micrometer grain size, 10% of the olivine may react within 3 years, 50% of the olivine may react within 18 years, and 90% of the olivine may react within 47 years. In contrast, for olivine with a 64 micrometer grain size, 10% of the olivine may react within 6 years, 50% of the olivine may react within 39 years, and 90% of the olivine may react within 101 years. The rates shown generally correspond to static dissolution rates based on inorganic chemical processes, and may not include acceleration of weathering due to wave energy and biotic processes. The systems and methods of the present disclosure may be implemented to optimize dissolution rates by (1) inducing or imparting wave energy with a specific characteristic (e.g., periodicity, intensity, motion path, etc.) and/or (2) modifying the biotic processes used to enhance olivine dissolution.\|[0078] FIG. 25 shows an exemplary modeling approach for particle distribution. In one step, the modeling approach may comprise simulating grains to match a desired particle size distribution. The modeling approach may further comprise shrinking each particle over a time period (e.g., to simulate dissolution or erosion of one or more portions or layers of each particle), and thereafter summing the total mass of the particles and/or the total amount dissolved or eroded at various time points in order to determine the fraction of mass remaining as a function of time.\|[0079] FIG. 26 shows dissolution rates for different mixtures of olivine having different mean grain sizes. In general, olivine mixtures with smaller mean grain sizes may have a shorter half-life (i.e., a shorter time period for half of the olivine mixture to dissolve under a particular set of conditions).\|[0080] FIG. 27 shows the impact of temperature and pH on half-life. In some cases, the half-life for olivine dissolution may decrease as temperature increases. In some cases, the half-life for olivine dissolution may increase as pH increases. In some embodiments, the systems and methods disclosed herein may be implemented to optimize temperatures and pHs for dissolution environments to shorten the half-life for olivine dissolution. In other embodiments, the systems and methods disclosed herein may be implemented to identify candidate locations with optimal temperatures and pHs for olivine dissolution environments to shorten the half-life for olivine dissolution.\|[0081] The systems and methods disclosed herein may be configured or implemented to overcome challenges relating to spatial and temporal heterogeneity, low signal/noise ratios due to slow dissolution of olivine, and variation in secondary mineral product generation. The systems and methods disclosed herein may also help to overcome verification challenges such as, for example, objective criteria for acceptance and verification of carbon credit sales, and how to influence such criteria to adapt them to coastal weathering processes.\|[0082] The present disclosure provides methods for performing MRV (i.e., the measurement, recording, and verification) of carbon capture and/or olivine dissolution. In some cases, the methods may comprise establishing a treatment site and a reference or baseline site. The methods may further comprise measuring alkalinity fluxes and/or other parameters at a network of discrete locations. In some cases, this may be repeated over time as olivine dissolves over a series of time points. The methods may further comprise interpolating in time and space to determine an overall dissolution rate across an area or a volume of the site. In some cases, the overall dissolution rate across the site may be determined in part using a numerical reaction transport model that provides a fit to the measured data.\|[0083] FIG. 28 shows examples of temporal factors and spatial factors that can vary for coastal ecosystems, many of which are extremely dynamic. Temporal factors may include, for example, diurnal factors (i.e., day/night variations), tides, seasonality, temperature, weather, and/or waves. Spatial factors may include, for example, position and hydrodynamics, depth, tides, sediment type, grain size, sediment organic carbon content, and/or bottom cover (e.g., sea grass, rocks, coral, etc.).\|[0084] In some cases, the methods disclosed herein may comprise assessing or evaluating temporal heterogeneity by measuring depth, temperature, salinity, pH, turbidity, chlorophyll concentrations, and/or dissolved oxygen concentrations over time. FIG. 29 shows plots of temporal heterogeneity of various characteristics for a target site, including depth, salinity, turbidity, temperature, dissolved, oxygen, and pH. In some cases, the target site for olivine distribution and dissolution may be chosen based on temporal heterogeneity relative to other candidate or baseline/reference sites.\|[0085] As shown in FIGs. 30 - 32, in some cases, the methods disclosed herein may comprise calculating alkalinity fluxes and measuring dissolution rates of olivine to secure carbon credits. Alkalinity fluxes induced by olivine may be determined by discerning changes in alkalinity fluxes due to olivine from other natural background fluxes. In some cases, other fluxes attributable to olivine, such as dissolved inorganic carbon (DIC) fluxes and fluxes of pCO2, may be determined based on a comparison of measured fluxes to natural background fluxes. The fluxes attributable to olivine dissolution and/or the natural background fluxes may be space and time dependent. Such variations over space and time may be simulated, modeled, tracked, and/or measured to ensure accurate calculation of fluxes attributable to olivine, as opposed to natural background fluxes.\|[0086] In another aspect, the present disclosure provides various methods for accounting for heterogeneity for MRV. FIG. 33 shows a summary of the MRV approaches described below at different scales of cost and complexity.\|[0087] Approach 1 - In some cases, the methods may involve using the shrinking core model described elsewhere herein for an approximate rate of dissolution. The dissolution rate and CO2/olivine ratio may be assumed or approximated.\|[0088] Approach 2 - Alternatively, mesocosm experiments may be utilized to determine regional olivine dissolution rates. In cases where olivine is deployed in a target site (e.g., a mesocosm or the natural environment), olivine tracers may be used to track olivine dissolution in order to model and refine in situ weathering rates. The present disclosure provides systems and methods to track the movement of olivine grains in a target site. The systems and methods of the present disclosure may be implemented to track olivine transport in a target site based on or using, for example, trace metal content, fluorescent dyes, and/or olivine-specific spectral properties. This may be a relatively inexpensive process that can be set up prior to obtaining regulatory permits. Further, this approach may be initially tested using a sealed, recirculating design that is configured to maintain and control spatiotemporal heterogeneity and further allow for temperature and/or lighting control.\|[0089] Approach 3 - In some cases, the mesocosm-based approaches described herein may be augmented with field data (e.g., in situ data obtained manually or automatically using one or more sensors). The data obtained using the one or more sensors (which one or more sensors may comprise any of the sensors described herein or any other sensors for obtaining any of the measurements referred to herein) may provide additional information to better quantify and track spatial and/or temporal variations in environmental conditions or parameters relating to olivine dissolution and coastal carbon capture.\|[0090] Approach 4 - In some cases, a numerical model may be constructed that allows for accurate simulation of spatial and temporal variations in background fluxes and olivine dissolution rates. This can help to correct for time and space dependent variations, and allow for the use of sparse observations or other information or data at discrete points (e.g., points in time and/or points in space) to calibrate, verify, and validate the model. The model may be built and implemented for one or more a priori simulations.\|[0091] In cases where olivine is deployed in the natural environment, olivine tracers may be used to track olivine dissolution in order to estimate, predict, model, and refine in situ weathering rates. The present disclosure provides systems and methods for tracking the movement or transport of olivine grains in the natural environment (e.g., in a target site in which the olivine is provided or introduced). The systems and methods of the present disclosure may be implemented to track olivine transport based on or using, for example, trace metal content, fluorescent dyes, and/or olivine-specific spectral properties. The trace metal content, the movement or dispersion of fluorescent dyes, and/or the olivine-specific spectral properties may be detected and tracked using any of the sensors described herein.\|[0092] FIG. 34 illustrates various examples of reaction-transport modeling studies that may be used to simulate sediment porewater profiles, solid-phase chemistry, and benthic fluxes. The simulations and studies may be tailored to project requirements, and can take into account secondary clay mineralogy and Cr and Ni speciation and cycling. The plots shown in FIG. 34 illustrate an exemplary numerical simulation of alkalinity profile and the effects of spreading a 2 centimeter (cm) thick layer of pure olivine sand on a beach sediment. In some cases, the alkalinity flux across the sediment-water interface may be monitored by (1) constructing biogeochemical models of olivine dissolution in sediments, (2) validating model performance using field measurements of sediment-water alkalinity flux (and other carbonate parameters), and (3) calculating CO2 capture, storage, or sequestration (by weight or volume) based on the thermodynamics of air-sea CO2 exchange.\|[0093] The systems and methods disclosed herein may be implemented using one or more sensors capable of measuring at optimal spatial and temporal resolutions. The sensors may obviate the need to use traditional, manual geochemical methods, which require labor intensive field sampling and returning of samples to labs for analysis and can involve significant costs. FIG. 35 shows various examples of sensors that can be used for MRV, including sensors configured to measure temperature, salinity, pH, pCO2, DIC, alkalinity, and/or wave impacts on sand. In some cases, a solid state sensor for simultaneous measurement of total alkalinity and pH of seawater (including seawater that does or does not comprise olivine) may be used. In some embodiments, a plurality of sensors for MRV may be deployed on a single system. In other embodiments, a plurality of sensors for MRV may be deployed on multiple separate systems. Additional examples of sensors are shown in FIG. 36, including silicate sensors, alkalinity sensors, CTDO sensors, Cytochips, dissolved inorganic carbon sensors, and nitrate sensors. In some cases, a 29Si isotopic tracer can be used to track olivine dissolution and simultaneous precipitation of secondary clays and carbonate phases. This can allow separation of total and net silicate dissolution.\|[0094] In some cases, the impacts of physical wave-driven weathering on beach sand and olivine dissolution may be measured or simulated. In some cases, this may involve measuring and analyzing 2-phase (i.e., sand-water) flow in the benthic boundary layer of a breaking wave. This may be modeled numerically or physically (e.g., using wave tanks). In some cases, specialized sensors for measuring turbulent energy dissipation (e.g., in a lab or directly on a beach) may be utilized to measure impacts of physical wave-driven weathering.\|[0095] FIG. 38 illustrates an approach to measuring CO2 removal that is enabled by way of the reactions shown in FIG. 37. In some cases, it may not be feasible to monitor the air to sea CO2 flux. Measuring air-sea CO2 fluxes can be challenging because the olivine dissolution signal is strongly muted by dilution with open ocean seawater. For instance, a 1 cm thick layer of olivine dissolving in 5 meters of water in a bay with a 4-hour residence time implies a ~ 1.3 µM increase in water column alkalinity. Measuring net CO2 flux can also be complicated by extreme seasonal and diurnal variations in ΔPCO2air-sea due to changes in local photosynthesis and respiration. Accordingly, in some embodiments, the systems and methods disclosed herein may be implemented to monitor alkalinity flux across the sediment-water interface.\|[0096] In some cases, the models described herein (which models may be generated for specific sites) may undergo validation. Such validation may involve determining olivine abundance, spatial distribution, and dissolution rates at one or more reference points in space or time. In some cases, the reference points may be arranged in a grid pattern. Validation may further involve crossvalidating measured and modeled alkalinity fluxes and olivine dissolution at reference points, and calculating alkalinity flux for a region or a project based on (i) a known mass or volume of olivine deployed and (ii) validated site-specific modeling. The models may be validated using one or more sensor measurements as described elsewhere herein. Once validated, the models may be used to determine or predict olivine dissolution, reaction fluxes, and/or carbon sequestration. In some cases, the models may be updated or refined based on additional sensor measurements captured over a period of time. In some cases, the models may be revalidated based on additional sensor measurements.\|[0097] FIG. 39 illustrates an approach to calculating CO2 sequestration from alkalinity flux based on an expression of how water DIC storage changes as a function of increasing alkalinity. Seawater carbonate chemistry may be controlled by pCO2, pH, DIC, and alkalinity. An isocapnic quotient may be computed based on a change in alkalinity relative to a change in DIC, at fixed conditions for pCO2, temperature, and salinity. In some cases, a 1 micromol increase in alkalinity may yield a 0.78-0.93 micromol DIC increase, which means that for every one ton of forsterite provided to a target site, 0.97 to 1.16 tons of CO2 can be stored as marine DIC.\|[0098] FIG. 40 illustrates a plot showing seawater age and the depth below sea water level of the Atlantic Ocean as a function of latitude (degrees North). CO2 capture via ocean alkalinization requires that the enhanced alkalinity water mass achieves equilibrium with atmospheric pCO2. The precise timescale for pCO2 equilibrium (~ 4 months) and DIC adjustment (~4 years) depends on the Revelle factor (Jones et al. 2014). The time scale for air-sea equilibration is considerably shorter than the time scale for olivine dissolution (~ 10 - 100 year) and approximately similar to the transit time distribution of mixed layer and subtropical mode water (- 10 - 40 years). This means that the surface DIC reservoir can achieve quasi-steady equilibrium throughout equatorial and subtropical regions most suitable for coastal enhanced weather.\|[0099] FIG. 41 illustrates an exemplary CEW life cycle analysis. The life cycle may comprise mining and/or extracting olivine, grinding the olivine to approximately 400 micrometer grain sizes (or less), transporting the olivine to one or more target sites, and spreading the olivine at the target sites. In some cases, the life cycle may be at least about 89% efficient, and can enable sequestration of at least about 5 to 20 times more CO2 than the amount of CO2 emitted during mining, grinding, transportation, and/or spreading of olivine.\|[0100] FIG. 42 illustrates an example of a carbon payback period that can be realized using the methods and systems disclosed herein. In some cases, the break even payback period may occur at approximately 4 years, assuming the following:\| Grainsize: LE45 (d50: 365 µm)\| Temp: 25 °C\| pH: 8\| Embedded emissions: 110 tons CO2 / 1000 tons olivine\| Absorption efficiency: 3 moles ALK / mole olivine\| Dissolution constant: Log(r) = - 8.75 (can vary depending on pH/temp)\|[0101] FIG. 43 illustrates various plots showing exemplary olivine dissolution kinetics for olivine particles having different grain sizes. Dissolution time may decrease as olivine particle sizes decrease. The particle dissolution characteristics may be predicted or simulated using a shrinking core model and one or more laws, equations, or principles governing olivine dissolution rates. In some cases, the shrinking core model may be modified to permit the simulation of dissolution for realistic, commercially-available grain size distributions. The models described herein may be generated by modifying initial diagenesis models to incorporate olivine dissolution kinetics that correspond to the shrinking core model. The models may include and/or account for full carbonate chemistry (e.g., DIC, ALK, pCO2, pH, carbonate precipitation/dissolution) as well as biogeochemical processes (including aerobic and anaerobic respiration, formation of Fe/Mn oxides, pyrite, sulfide oxidation, etc).\|[0102] In some instances, secondary carbonate precipitation as shown in FIG. 44 can impact CO2 capture efficiency. Secondary carbonate precipitation may change the reactions described herein such that for every 1 mol of olivine introduced to a target environment, 2 moles of CO2 are consumed and 0 moles of alkalinity are generated. This can result in a 50% reduction in CO2 capture efficiency. The systems and methods disclosed herein may be implemented to minimize or reduce secondary carbonate precipitation. The rate of carbonate precipitation can be strongly controlled by local variations in geochemistry and biogenic calcification. In some cases, alkalinity export can be the dominant process occurring in sediments, and once mixed into the water column, consumption of alkalinity can be low given the long residence time of DIC and ALK in seawater.\|[0103] In some instances, secondary clay formation as shown in FIG. 45 can impact CO2 capture efficiency. Secondary clay formation may change the reactions described herein such that for every 1 mol of olivine, 8/3 moles of CO2 are consumed and 8/3 moles of alkalinity are generated. This can result in a 33% reduction in CO2 capture efficiency. The systems and methods disclosed herein may be implemented to minimize or reduce such secondary clay formation.\|[0104] In a related aspect, the present disclosure provides systems and methods for simulating a target site or environment. This can allow the study of olivine dissolution rates in a controlled environment, intermediate between lab and field conditions. Such systems and methods may be implemented to determine and/or monitor olivine dissolution rates, porewater geochemistry, or benthic flux measurements, study impacts of temperature on olivine dissolution and respiration, track impacts on seawater pH and other water chemistry, monitor ecological responses and air-sea water gas CO2 fluxes, track the fate, transport, and bioaccumulation of Cr and Ni, track the formation of secondary weathering products (e.g., Chrysotile, Carbonates, Clays), and monitor the impacts of olivine-based CO2 sequestration processes on benthic invertebrates/meiofauna.\|[0105] In some embodiments, the MRV methods and protocols disclosed herein may be adapted or adjusted for different types of olivine or for different target sites for olivine distribution. In such cases, the models used to predict or determine olivine dissolution, reaction fluxes, and/or carbon sequestration may be adjusted based on characteristics of the particular olivine/sand mixture used, the target site, and/or one or more sensor readings or measurements obtained in situ.\|Carbon Removal Prediction\|[0106] [6] In another aspect, the present disclosure provides systems and methods for predicting rates of carbon removal at specific sites. Such predictions may be based on, for example, data corresponding to measurement of changes in alkalinity, pCO2, pH, and/or water temperature. The predictions may be generated using algorithms and software interpreting such data. The algorithms and software may be implemented by way of one or more models that can be generated based on the MRV data obtained using various sensors as described elsewhere herein.\|[0107] In some embodiments, the predicted rates of carbon removal may be used to further optimize the carbon capture process. For instance, the predicted rates may be used to optimize the properties of the olivine sand, the preparation of the olivine sand, and/or the operation or the configuration of the reactor.\|Shipping and Deployment of Olivine\|[0108] [7] In another aspect, the present disclosure provides systems and methods for shipping and deploying olivine. In some cases, the shipping and deployment of olivine may be performed using a device for distributing carbon negative sand in shallow marine environments. The device may be, for example, a spreading device for spreading the olivine in a desired or optimal manner at a target site (e.g., a beach of interest).\|[0109] In some cases, the methods of the present disclosure may comprise determining whether one or more dredging modifications are needed in order to optimally distribute the carbon negative sand. Such determination may be based on one or more sensor readings and/or information about the target site in which the carbon negative sand is to be distributed.\|[0110] In some cases, the olivine may be processed before shipping to facilitate shipping and distribution of the olivine. For instance, the olivine may be modified to enable transportation of ultra-fine material (e.g., for reduction of liquefaction or capsizing risk.\|[0111] In some embodiments, various types and forms of maritime emissions reduction technology (e.g., an on-board olivine reactor driven by ship engine using ballast water) may be implemented. In some cases, bulk carrier direct deployment technology and related modifications (e.g., open sea distribution for in situ CEW) may be utilized. In some cases, grain washing and liquid alkalinity systems may be used for pre-deployment reduction of turbidity. In some cases, global logistics software may be used to mobilize idle maritime assets for carbon removal projects.\|[0112] FIG. 9 schematically illustrates an example of a system that may be used to deploy olivine for coastal nourishment. The system may comprise, for example, a split hulled hopper barge. In some cases, olivine may be mined and milled into carbon negative sand. Thereafter, the olivine may be loaded and shipped on dry bulk carriers to designated ports. The olivine may then be loaded into one or more split hulled hopper barges. In some embodiments, the barges may be linked together and towed to designated deployment sites. Once the barges are positioned at or near the designated deployment sites, the bottom of the barges may be configured to open in order to deploy the olivine. In some cases, sediment transport modeling may be used to predict where the olivine will move and/or in what directions the olivine will disperse.\|[0113] In a further aspect, the present disclosure provides a method and process for conducting carbon neutral and carbon negative dredging operations. The method and process of conducting dredging operations may be either net neutral or net negative with respect to atmospheric greenhouse gas emissions. To achieve this, dredged sediment may be mixed with one or more types of carbon negative sand, as described elsewhere herein. The methods and processes described herein may be adapted for any type of construction activity, including land-based construction activities.\|[0114] The dissolution of carbon negative sand may effect the conversion of gaseous and dissolved carbon dioxide into dissolved bicarbonate and carbonate ions, thereby increasing the capacity of fresh and salt water to store additional carbon in a dissolved state. When present as dissolved bicarbonate and carbonate ions, rather than carbon dioxide, these compounds may no longer contribute to climate change and can act to counter the effect of ocean acidification.\|[0115] In order to reduce, neutralize, or negate carbon dioxide emissions which occur during the combustion of fossil fuels during conventional dredging operations, a predefined ratio of carbon negative sand may be mixed with the dredging spoils in order to [1] result in the net capture of a specified amount of carbon dioxide and [2] ensure that the dredged sediments meet engineering and regulatory requirements for disposal or beneficial reuse. Blends consisting of 1-50% reactive carbon negative component may be most common, but in other variations, higher or lower fractions of the carbon negative component may be used.\|[0116] In order to mix carbon negative sand with dredged materials, several different approaches may be used depending on the type of dredging operation and intended fate of the dredged material. During cutterhead dredging operations, pump-out hopper dredging, and other approaches where dredged material is conveyed via a hydrologic slurry, the carbon negative sand may be directly mixed with the dredge spoils by injecting the carbon negative sand into the slurry pipeline. When using trailing suction hopper dredges, carbon negative sand may be mixed within a sediment hopper or barge prior to discharge. As an alternative, carbon negative sand may be directly placed at the sediment destination in the specified quantity and allowed to mix with the dredge spoils via the action of wind, waves, tides, and currents.\|[0117] Whereas traditional dredging operations consume large quantities of fuel fuels and emit correspondingly large quantities of greenhouse gasses, the method and process described here may allow dredging operations to be conducted in a way that is carbon neutral or even carbon negative over the lifetime of the project. This method and process provides significant advantages, allowing dredging operators to (i) mitigate carbon dioxide emissions on behalf of themselves or their clients, (ii) avoid emissions caps and taxes, and (iii) operate in jurisdictions which impose voluntary or involuntary restrictions on greenhouse gas emissions.\|Carbon-removing marine landfill cap\|[0118] In another aspect, the present disclosure provides carbon-removing marine landfill caps, processes for making the same, and processes for quantifying carbon capture from carbon-removing marine landfill caps. Marine landfills may serve as long-term, seafloor placement areas for unwanted construction debris, dredging materials, and toxic pollutants. Currently, marine landfills are often "capped" with non-toxic clay or sand or other similar materials to prevent contamination of overlying seawater and allow marine life to thrive in previously environmentally damaged areas. By using carbon-removing sand wholly, or as a constituent of, marine landfill caps, these sites can serve as climate change mitigation locales and further encourage the regeneration of environmentally damaged areas through the production of bicarbonate (alkalinity) which offsets ocean acidification and is beneficial for marine life.\|[0119] The process of making and deploying carbon-removing marine landfill cap differs from traditional marine landfill cap because 1) the depth (thickness) of carbon-removing cap sand 2) grain size distribution of carbon-removing cap sand, and 3) possible blend of carbon-removing cap and standard cap must be optimized to 1) prevent release of toxic pollutants and similar while allowing for sufficient permeability so that the carbon-removing sand will capture carbon over time and in particular not saturate sand porewaters such that the carbon removal reaction slows or stops. To achieve these objectives, a carbon-removing marine landfill cap may be deployed wholly as a cap, applied as a single mixture of carbon-removing cap to regular cap sand, or applied in layers where the percentage of carbon-removing cap sand to regular cap sand changes with depth, or the grain size distribution of carbon-removing cap and/or standard cap changes with depth. In all circumstances the carbon capture rates may vary with depth. In some cases, the carbon capture rate may be determined based on analytical measurements and sensor measurements from a particular site, fit to a global model. In some embodiments, the appropriate deployment technique described above may be a function of local wave climate, ecology (bioturbation), seawater temperature, landfill material, and an LCA (life cycle analysis) as the CO2 emitted to deploy the carbon-removing cap must be accounted for to insure the cap is, indeed, carbon-removing.\|Green Hydrogen\|[0120] [8] In another aspect, the present disclosure provides systems and methods for generating and using green hydrogen. As used herein, the term "green hydrogen" may refer to hydrogen that is produced from renewable energy sources and/or low-carbon power sources. The green hydrogen may be used as fuel for fuel cells or internal combustion engines. In some cases, the green hydrogen may be generated based on one or more products or reactants used to drive the CO2 capture and sequestration reactions/methods described elsewhere herein.\|Computer Systems\|[0121] In an aspect, the present disclosure provides computer systems that are programmed or otherwise configured to implement methods of the disclosure, e.g., any of the subject methods for processing and distributing olivine. FIG. 10 shows a computer system 1001 that is programmed or otherwise configured to implement a method for olivine processing and distribution. The computer system 1001 may be configured to, for example, (i) identify a target site, (ii) optimize one or more procedures for processing olivine to yield favorable properties or characteristics for the olivine, based on the target site identified, and (iii) coordinate transportation of the olivine to the target site. The computer system 1001 can be an electronic device of a user or a computer system that is remotely located with respect to the electronic device. The electronic device can be a mobile electronic device.\|[0122] The computer system 1001 may include a central processing unit (CPU, also "processor" and "computer processor" herein) 1005, which can be a single core or multi core processor, or a plurality of processors for parallel processing. The computer system 1001 also includes memory or memory location 1010 (e.g., random-access memory, read-only memory, flash memory), electronic storage unit 1015 (e.g., hard disk), communication interface 1020 (e.g., network adapter) for communicating with one or more other systems, and peripheral devices 1025, such as cache, other memory, data storage and/or electronic display adapters. The memory 1010, storage unit 1015, interface 1020 and peripheral devices 1025 are in communication with the CPU 1005 through a communication bus (solid lines), such as a motherboard. The storage unit 1015 can be a data storage unit (or data repository) for storing data. The computer system 1001 can be operatively coupled to a computer network ("network") 1030 with the aid of the communication interface 1020. The network 1030 can be the Internet, an internet and/or extranet, or an intranet and/or extranet that is in communication with the Internet. The network 1030 in some cases is a telecommunication and/or data network. The network 1030 can include one or more computer servers, which can enable distributed computing, such as cloud computing. The network 1030, in some cases with the aid of the computer system 1001, can implement a peer-to-peer network, which may enable devices coupled to the computer system 1001 to behave as a client or a server.\|[0123] The CPU 1005 can execute a sequence of machine-readable instructions, which can be embodied in a program or software. The instructions may be stored in a memory location, such as the memory 1010. The instructions can be directed to the CPU 1005, which can subsequently program or otherwise configure the CPU 1005 to implement methods of the present disclosure. Examples of operations performed by the CPU 1005 can include fetch, decode, execute, and writeback.\|[0124] The CPU 1005 can be part of a circuit, such as an integrated circuit. One or more other components of the system 1001 can be included in the circuit. In some cases, the circuit is an application specific integrated circuit (ASIC).\|[0125] The storage unit 1015 can store files, such as drivers, libraries and saved programs. The storage unit 1015 can store user data, e.g., user preferences and user programs. The computer system 1001 in some cases can include one or more additional data storage units that are located external to the computer system 1001 (e.g., on a remote server that is in communication with the computer system 1001 through an intranet or the Internet).\|[0126] The computer system 1001 can communicate with one or more remote computer systems through the network 1030. For instance, the computer system 1001 can communicate with a remote computer system of a user (e.g., an end user performing or monitoring the processing and/or the transportation or distribution of the olivine). Examples of remote computer systems include personal computers (e.g., portable PC), slate or tablet PC's (e.g., Apple® iPad, Samsung® Tab), telephones, Smart phones (e.g., Apple® iPhone, Android-enabled device, Blackberry®), or personal digital assistants. The user can access the computer system 1001 via the network 1030.\|[0127] Methods as described herein can be implemented by way of machine (e.g., computer processor) executable code stored on an electronic storage location of the computer system 1001, such as, for example, on the memory 1010 or electronic storage unit 1015. The machine executable or machine readable code can be provided in the form of software. During use, the code can be executed by the processor 1005. In some cases, the code can be retrieved from the storage unit 1015 and stored on the memory 1010 for ready access by the processor 1005. In some situations, the electronic storage unit 1015 can be precluded, and machine-executable instructions are stored on memory 1010.\|[0128] The code can be pre-compiled and configured for use with a machine having a processor adapted to execute the code, or can be compiled during runtime. The code can be supplied in a programming language that can be selected to enable the code to execute in a pre-compiled or ascompiled fashion.\|[0129] Aspects of the systems and methods provided herein, such as the computer system 1001, can be embodied in programming. Various aspects of the technology may be thought of as "products" or "articles of manufacture" typically in the form of machine (or processor) executable code and/or associated data that is carried on or embodied in a type of machine readable medium. Machine-executable code can be stored on an electronic storage unit, such as memory (e.g., read-only memory, random-access memory, flash memory) or a hard disk. "Storage" type media can include any or all of the tangible memory of the computers, processors or the like, or associated modules thereof, such as various semiconductor memories, tape drives, disk drives and the like, which may provide non-transitory storage at any time for the software programming. All or portions of the software may at times be communicated through the Internet or various other telecommunication networks. Such communications, for example, may enable loading of the software from one computer or processor into another, for example, from a management server or host computer into the computer platform of an application server. Thus, another type of media that may bear the software elements includes optical, electrical and electromagnetic waves, such as used across physical interfaces between local devices, through wired and optical landline networks and over various air-links. The physical elements that carry such waves, such as wired or wireless links, optical links or the like, also may be considered as media bearing the software. As used herein, unless restricted to non-transitory, tangible "storage" media, terms such as computer or machine "readable medium" refer to any medium that participates in providing instructions to a processor for execution.\|[0130] Hence, a machine readable medium, such as computer-executable code, may take many forms, including but not limited to, a tangible storage medium, a carrier wave medium or physical transmission medium. Non-volatile storage media including, for example, optical or magnetic disks, or any storage devices in any computer(s) or the like, may be used to implement the databases, etc. shown in the drawings. Volatile storage media include dynamic memory, such as main memory of such a computer platform. Tangible transmission media include coaxial cables; copper wire and fiber optics, including the wires that comprise a bus within a computer system. Carrier-wave transmission media may take the form of electric or electromagnetic signals, or acoustic or light waves such as those generated during radio frequency (RF) and infrared (IR) data communications. Common forms of computer-readable media therefore include for example: a floppy disk, a flexible disk, hard disk, magnetic tape, any other magnetic medium, a CD-ROM, DVD or DVD-ROM, any other optical medium, punch cards paper tape, any other physical storage medium with patterns of holes, a RAM, a ROM, a PROM and EPROM, a FLASH-EPROM, any other memory chip or cartridge, a carrier wave transporting data or instructions, cables or links transporting such a carrier wave, or any other medium from which a computer may read programming code and/or data. Many of these forms of computer readable media may be involved in carrying one or more sequences of one or more instructions to a processor for execution.\|[0131] The computer system 1001 can include or be in communication with an electronic display 1035 that comprises a user interface (UI) 1040 for providing, for example, a portal for a user to monitor the processing and/or the transportation or distribution of the olivine. The portal may be provided through an application programming interface (API). A user or entity can also interact with various elements in the portal via the UI. Examples of UI's include, without limitation, a graphical user interface (GUI) and web-based user interface.\|[0132] Methods and systems of the present disclosure can be implemented by way of one or more algorithms. An algorithm can be implemented by way of software upon execution by the central processing unit 1005. For example, the algorithm may be configured to identify a target site and optimize a procedure for processing the olivine based on the properties or the characteristics of the target site.\|[0133] While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. It is not intended that the invention be limited by the specific examples provided within the specification. While the invention has been described with reference to the aforementioned specification, the descriptions and illustrations of the embodiments herein are not meant to be construed in a limiting sense. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. Furthermore, it shall be understood that all aspects of the invention are not limited to the specific depictions, configurations or relative proportions set forth herein which depend upon a variety of conditions and variables. It should be understood that various alternatives to the embodiments of the invention described herein may be employed in practicing the invention. It is therefore contemplated that the invention shall also cover any such alternatives, modifications, variations or equivalents. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby.	(EP4166641)\|CROSS REFERENCE\|[0001] This application claims priority to U.S. Provisional Patent Application No. 63/256,986 filed on October 18, 2021, U.S. Provisional Patent Application No. 63/281,575 filed on November 19, 2021, and U.S. Provisional Patent Application No. 63/298,412 filed on January 11, 2022, each of which is incorporated herein by reference in its entirety for all purposes.\|BACKGROUND\|[0002] Enhanced weathering or accelerated weathering may be used to remove atmospheric carbon dioxide by leveraging natural or artificially created minerals that can absorb and transform carbon dioxide into other substances through chemical reactions that may occur in the presence of water (e.g., in the form of rain, groundwater or seawater).\|SUMMARY\|[0003] The present invention relates to a system for processing olivine. More specifically, the present invention relates to a system for processing olivine wherein the system comprises a reactor for accelerating olivine weathering, more particularly, the reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering. Enhanced weathering may be used in marine environments to increase ocean alkalinity and atmospheric CO2 uptake. In some cases, enhanced weather may involve adding processed minerals directly to the ocean or dumping the processed minerals on beaches where wave action can disperse the processed minerals into the target marine environment. Enhanced weathering may be used to reduce CO2 levels in the atmosphere while also counteracting ocean acidification.\|[0004] Recognized herein are various limitations with current weathering methods, which may (i) involve long lead times and labor intensive procedures, (ii) impact ecological conditions (e.g., increasing water turbidity), and (iii) handling/processing of minerals that can pose additional ecological and health hazards via the possible ingestion, contact, or inhalation of fine grain of olivine mineral dust.\|[0005] The present application relates generally to using olivine to achieve enhanced weathering and increase CO2 uptake on accelerated timescales. In one aspect, the present disclosure provides systems and methods for accelerating weathering. In another aspect, the present disclosure provides a bioreactor configured to accelerate dissolution of olivine for weathering applications. In a further aspect, the present disclosure provides systems and methods for enhancing material properties of olivine. For example, the present disclosure provides a way to optimize the surface area effect of fine olivine grains by utilizing a binding process to bind or encapsulate the olivine fines into pellets of a larger effective grain size which can be more safely handled and distributed in the environment. The ability to tailor the design of pellets composed of olivine mineral fines by using different binding agents or encapsulation processes provides the ability to tailor and control the porosity, permeability, and degradation characteristics of the olivine-containing pellets, controlling their dissolution behavior in the environment. The systems and methods disclosed herein may enable efficient processing and deployment of olivine for purposes of CO2 capture in marine environments.\|[0006] In some embodiments, pelletized olivine aggregates formed from olivine fines may be prepared through a number of processes disclosed herein including [1] the use of a binding agent (such as but not limited to clay, polysaccharides, proteinaceous compounds, resin, plastic, glass, etc.) [2] via encapsulation of smaller olivine grains with said binding agent or other similar materials or [3] via the thermal fusion or physical compression of smaller olivine grains into larger aggregates.\|[0007] In some embodiments, the pellets may be designed to either [4] remain substantially intact while maintaining improved surface area via internal porosity and permeability or [5] degrade in a controlled fashion to release fine olivine fines to the environment in a prolonged controlled fashion. In some cases, [6] the preparation of such pellets may allow olivine dissolution to occur substantially faster than would occur for equivalently sized solid pure olivine grains, thereby improving the process of carbon capture while minimizing the aesthetic, health, and ecological harm and challenges posed by working with and utilizing olivine mineral fines.\|[0008] Another aspect of the present disclosure provides a non-transitory computer readable medium comprising machine executable code that, upon execution by one or more computer processors, implements any of the methods above or elsewhere herein.\|[0009] Another aspect of the present disclosure provides a system comprising one or more computer processors and computer memory coupled thereto. The computer memory comprises machine executable code that, upon execution by the one or more computer processors, implements any of the methods above or elsewhere herein.\|[0010] Additional aspects and advantages of the present disclosure will become readily apparent to those skilled in this art from the following detailed description, wherein only illustrative embodiments of the present disclosure are shown and described. As will be realized, the present disclosure is capable of other and different embodiments, and its several details are capable of modifications in various obvious respects, all without departing from the disclosure. Accordingly, the drawings and description are to be regarded as illustrative in nature, and not as restrictive.\|INCORPORATION BY REFERENCE\|[0011] All publications, patents, and patent applications mentioned in this specification are herein incorporated by reference to the same extent as if each individual publication, patent, or patent application was specifically and individually indicated to be incorporated by reference. To the extent publications and patents or patent applications incorporated by reference contradict the disclosure contained in the specification, the specification is intended to supersede and/or take precedence over any such contradictory material.\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0012] The novel features of the invention are set forth with particularity in the appended claims. A better understanding of the features and advantages of the present invention will be obtained by reference to the following detailed description that sets forth illustrative embodiments, in which the principles of the invention are utilized, and the accompanying drawings (also "Figure" and "FIG." herein), of which:\| FIG. 1 schematically illustrates the long-term carbonate-silicate cycle, in accordance with some embodiments.\| FIG. 2 schematically illustrates the chemical processes by which olivine can be used to capture and sequester CO2, in accordance with some embodiments.\| FIG. 3 schematically illustrates the chemical reactions that enable CO2 capture and sequestration using olivine, in accordance with some embodiments.\| FIG. 4 schematically illustrates olivine and mixtures of sand and olivine, in accordance with some embodiments.\| FIG. 5 schematically illustrates one exemplary method for using olivine to remove atmospheric CO2 and increase ocean alkalinity, in accordance with some embodiments.\| FIG. 6 schematically illustrates the use of wave energy to cause sand grains and/or olivine grains to collide and break into smaller pieces, thereby facilitating the dissolution of olivine, in accordance with some embodiments.\| FIG. 7 schematically illustrates an example of how the oceans can be used for natural carbon storage, in accordance with some embodiments.\| FIG. 8 schematically illustrates an example of a bioreactor, in accordance with some embodiments.\| FIG. 9 schematically illustrates an example of a system for deploying olivine for coastal nourishment, in accordance with some embodiments.\| FIG. 10 schematically illustrates a computer system that is programmed or otherwise configured to implement methods provided herein.\| FIG. 11 schematically illustrates an exemplary reactor configured to intake seawater that may be mixed with olivine and microbial biomass to generate alkalinity.\| FIG. 12 schematically illustrates an exemplary protocol for measuring, recording, and verifying (MRV) carbon removal, in accordance with some embodiments.\| FIGs. 13 - 14 schematically illustrate a chemical reaction by which coastal carbon capture occurs when olivine is introduced to a target site, in accordance with some embodiments.\| FIGs. 15 - 20 schematically illustrate an environment in which olivine can be introduced for costal carbon capture, in accordance with some embodiments.\| FIGs. 21A and 21B schematically illustrates a plot of concentration of an alkaline material in a flux chamber as a function of time, in accordance with some embodiments.\| FIG. 22 schematically illustrates an overview of the porewater method, in accordance with some embodiments.\| FIG. 23 schematically illustrates a shrinking core model, in accordance with some embodiments.\| FIG. 24 schematically illustrates dissolution rates for olivine having various grain sizes, in accordance with some embodiments.\| FIG. 25 schematically illustrates an exemplary modeling approach for particle distribution, in accordance with some embodiments.\| FIG. 26 schematically illustrates dissolution rates for different mixtures of olivine having different mean grain sizes, in accordance with some embodiments.\| FIG. 27 schematically illustrates the impact of temperature and pH on olivine half-life, in accordance with some embodiments.\| FIG. 28 schematically illustrates examples of temporal factors and spatial factors that can vary for coastal ecosystems, in accordance with some embodiments.\| FIG. 29 schematically illustrates plots of the temporal heterogeneity of various characteristics for a target site, in accordance with some embodiments.\| FIGs. 30 - 32 schematically illustrate examples of factors to consider when calculating alkalinity fluxes, in accordance with some embodiments.\| FIG. 33 shows a summary of various approaches for measuring, recording, and verifying carbon capture and olivine dissolution at different scales of cost and complexity, in accordance with some embodiments.\| FIG. 34 schematically illustrates various reaction-transport modeling studies that may be used to simulate sediment porewater profiles, solid-phase chemistry, and benthic fluxes, in accordance with some embodiments.\| FIGs. 35 - 36 schematically illustrate various examples of sensors that can be used for measuring, recording, and verifying carbon capture and/or olivine dissolution, in accordance with some embodiments.\| FIGs. 37 - 38 schematically illustrate reactions that may occur when olivine sand is introduced to beaches, in accordance with some embodiments.\| FIG. 39 schematically illustrates an approach to calculating CO2 sequestration from alkalinity flux based on an expression of how water DIC storage changes as a function of increasing alkalinity, in accordance with some embodiments.\| FIG. 40 schematically illustrates a plot showing seawater age and the depth below sea water level of the Atlantic Ocean as a function of latitude (degrees North), in accordance with some embodiments.\| FIG. 41 schematically illustrates an exemplary coastal enhanced weathering (CEW) life cycle analysis, in accordance with some embodiments.\| FIG. 42 schematically illustrates an example of a carbon payback period that can be realized using the methods and systems disclosed herein, in accordance with some embodiments.\| FIG. 43 schematically illustrates various plots showing exemplary olivine dissolution kinetics for olivine particles having different grain sizes, in accordance with some embodiments.\| FIG. 44 schematically illustrates the effects of secondary carbonate precipitation on CO2 capture efficiency, in accordance with some embodiments.\| FIG. 45 schematically illustrates the effects of secondary clay formation on CO2 capture efficiency, in accordance with some embodiments.\|DETAILED DESCRIPTION\|[0013] While various embodiments of the invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. Numerous variations, changes, and substitutions may occur to those skilled in the art without departing from the invention. It should be understood that various alternatives to the embodiments of the invention described herein may be employed.\|[0014] Whenever the term "at least," "greater than," or "greater than or equal to" precedes the first numerical value in a series of two or more numerical values, the term "at least," "greater than" or "greater than or equal to" applies to each of the numerical values in that series of numerical values. For example, greater than or equal to 1, 2, or 3 is equivalent to greater than or equal to 1, greater than or equal to 2, or greater than or equal to 3.\|[0015] Whenever the term "no more than," "less than," or "less than or equal to" precedes the first numerical value in a series of two or more numerical values, the term "no more than," "less than," or "less than or equal to" applies to each of the numerical values in that series of numerical values. For example, less than or equal to 3, 2, or 1 is equivalent to less than or equal to 3, less than or equal to 2, or less than or equal to 1.\|[0016] The term "real time" or "real-time," as used interchangeably herein, generally refers to an event (e.g., an operation, a process, a method, a technique, a computation, a calculation, an analysis, a visualization, an optimization, etc.) that is performed using recently obtained (e.g., collected or received) data. In some cases, a real time event may be performed almost immediately or within a short enough time span, such as within at least 0.0001 millisecond (ms), 0.0005 ms, 0.001 ms, 0.005 ms, 0.01 ms, 0.05 ms, 0.1 ms, 0.5 ms, 1 ms, 5 ms, 0.01 seconds, 0.05 seconds, 0.1 seconds, 0.5 seconds, 1 second, or more. In some cases, a real time event may be performed almost immediately or within a short enough time span, such as within at most 1 second, 0.5 seconds, 0.1 seconds, 0.05 seconds, 0.01 seconds, 5 ms, 1 ms, 0.5 ms, 0.1 ms, 0.05 ms, 0.01 ms, 0.005 ms, 0.001 ms, 0.0005 ms, 0.0001 ms, or less.\|Overview\|[0017] To avoid the worst effects of climate change, we must rapidly remove billions of tons of CO2 from the atmosphere. There are currently no proven methods for doing so. There is an urgent need to identify carbon removal methods that are permanent, scalable, and economical.\|[0018] The earth's natural long-term carbonate-silicate cycle is how our planet has naturally captured CO2 over thousands of years. Over millennia, rain falling on exposed volcanic rock causes it to weather, which removes CO2 from the atmosphere as bicarbonate dissolved in water. This water flows to the oceans, where marine calcifying organisms incorporate the CO2 into their shells and skeletons. When they die, they form ocean sediment, ultimately becoming limestone.\|[0019] The systems and methods of the present disclosure enable the acceleration of Earth's natural carbon removal method of rock weathering, through the extraction, processing (e.g., crushing and/or grinding), and transportation of volcanic mineral olivine to coastlines for dispersal or distribution. In some embodiments, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process. In other embodiments, a bioreactor may be used to enhance and facilitate olivine dissolution. In either case, carbon dioxide may be removed from the atmosphere as the olivine breaks down.\|[0020] Coastal Carbon Capture, also known as Coastal Enhanced Weathering, can be categorized as a negative emission technology (NET) that removes and stores CO2 on long timescales (tens to hundreds of thousands of years). The process aims to accelerate the natural chemical weathering of the mineral olivine by spreading large amounts of ground olivine-containing rock onto coastlines or bioreactors positioned on or near such coastlines, where it can dissolve in seawater, thereby increasing the rate of CO2 absorption by the ocean.\|[0021] The present disclosure provides systems and methods for accelerating the Earth's natural carbon removal method of rock weathering, by extracting the volcanic mineral olivine, grinding it into sand, and deploying it on coastlines or in bioreactors located on said coastlines. There, wave energy may cause the olivine particles to collide, grinding each other up and dramatically accelerating the weathering process. Carbon dioxide is removed from the atmosphere as the olivine breaks down.\|[0022] FIG. 1 illustrates the long-term carbonate-silicate cycle. The illustrated reaction is the foundation of the Long-Term Inorganic Carbon Cycle, which has been occurring for billions of years, stabilizing Earth's atmospheric CO2 concentrations, and in turn enabling life to thrive. In fact, carbon dioxide removal (CDR) through natural rock weathering consumes ~1 gigaton of CO2 every year. Natural CO2 removal through rock weathering may be achieved through the following steps:\| 1. Rain falls on volcanic rocks, slowly dissolving them.\| 2. Carbonic acid dissolved in the rainwater reacts with silicate from the rocks, shifting the equilibrium from carbonic acid to bicarbonate.\| 3. This bicarbonate flows to the ocean.\| 4. Marine organisms use this as calcium carbonate in their shells and skeletons; when they die this becomes limestone.\| 5. Limestone formed at the ocean floor eventually subducts, locking up the carbon for millions of years.\|[0023] FIG. 2 illustrates the chemical processes that are enabled by olivine to perform CO2 capture and sequestration. FIG. 3 illustrates the chemical reactions that enable CO2 capture and sequestration using olivine. As the olivine dissolves, its products are magnesium ions (the second most abundant ion in the ocean behind sodium), silicate (used by diatoms to build their skeletons) and dissolved carbon. Referring to FIG. 2 and FIG. 3, when olivine dissolves in water, it drives the illustrated reaction, thus increasing CO2 uptake, raising pH, and generating alkalinity. As a result, this process has the potential co-benefit of counteracting ocean acidification. Ocean acidification is the process by which increasing atmospheric CO2 dissolves in seawater, which reduces pH (increasing acidity) (upper reaction in diagram below). This reduces the ability of calcifying organisms like corals to grow and produce exoskeletons, or shells. As shown in FIG. 2 and FIG. 3, dissolving olivine in water sequesters hydrogen ions into dissolved silicate (H4SiO4), a molecule that can be used by diatoms, an important photosynthesizing algae that fixes carbon dioxide and forms the base of food web.\|[0024] Unfortunately, natural chemical weathering happens too slowly to balance human CO2 emissions and is already accounted for in Earth's present-day carbon budget. The systems and methods disclosed herein can be deployed and implemented to accelerate this natural process to remove at least a gigaton of atmospheric CO2 per year on a global scale.\|Accelerating a Natural Process\|[0025] Coastal Carbon Capture can be used to accelerate Earth's natural CO2 removal process. At current rates, the natural process of rock weathering through rainfall needs to be sped up by at least 100 times to absorb the CO2 emitted by human activity. Coastal Carbon Capture (CCC) can accelerate the process by using wave energy and/or bioreactors to break down olivine. The rock containing the olivine may be placed in high-energy coastal environments, where wave energy mechanically activates the rock, causing collisions which remove the silica coating and efficiently grind the olivine down. The olivine sand then dissolves in the water at a rate orders of magnitude faster than in the geological process.\|[0026] Coastal Carbon Capture may comprise the following steps:\| 1. Extract olivine and efficiently grind it. Olivine is a green volcanic silicate mineral. It is highly abundant and found near the surface all over the world. Olivine rocks can be efficiently crushed to sand and gravel grain sizes.\| 2. Transport olivine to a nearby coastal area. The olivine sand may be transported (e.g., by rail, ship, or truck) to a nearby coastal shelf sea. There, it may be spread in a thin layer.\| 3. Wave energy may accelerate CO2 removal. Wave energy and currents may further grind down the olivine. Grain-on-grain collisions can cause fine fraction particles (< 10 microns) to form, which then weather very rapidly. The olivine may consequently dissolve in the water rapidly, accelerating the reaction which removes CO2 from the ocean/atmosphere.\|[0027] FIG. 5 illustrates one exemplary method for using olivine to remove atmospheric CO2 and increase ocean alkalinity. As shown in FIG. 6, wave energy may cause sand grains and/or olivine grains to collide and break into smaller pieces, thereby facilitating the dissolution of olivine.\|Olivine\|[0028] Olivine is a common, naturally occurring volcanic mineral, with physical properties similar to quartz. Olivine may be 23% denser than quartz sand (1.43 tons/cy). Olivine sand is a clean upland sand that is 25% denser than silicate sand, and that can be artificially milled to match native grain size. Darker and lighter olivine sources allow for color matching to the native sand color.\|[0029] Olivine can be processed to yield fine olivine grains with increased surface area exposure, which can speed up dissolution and the CO2 capture process. The olivine dissolution and CO2 capture process can also be accelerated by (i) using reactive and soluble minerals, (ii) increasing an amount of surface area of the olivine grains that is exposed to a solvent (e.g., water or seawater), (iii) enhancing fluid-mineral interactions, and/or (iv) reducing or eliminating secondary mineral coatings or the formation of secondary weathering products (e.g., precipitation of secondary clays and carbonate phases).\|[0030] Once deployed on a beach, olivine can capture 20 times more carbon than is emitted in the mining, milling, shipping, and beach nourishment operation. 1 ton of olivine sand can capture up to 1.25 tons of carbon in ideal situations. Since it takes olivine several decades to weather, it will provide effective coastal protection during long-term beach nourishment cycles.\|[0031] One type of olivine may be white olivine, or Forsterite (Mg2SiO4). This is a magnesium rich form of olivine, known as Forsterite (Mg2SiO4). Weathering 1 ton of olivine can remove up to 1.25 tons of CO2 from the atmosphere.\|[0032] FIG. 4 illustrates olivine and mixtures of sand and olivine. In some cases, the olivine may be mixed with natural beach sand before the olivine is deployed at a target site. The mixture comprising the olivine may comprise at least about 5%, 10%, 15%, 20%, 25%, or 30% olivine by weight or volume. In some cases, the mixture may comprise more than 30% olivine by weight or volume. In some cases, the mixture may comprise less than 5% olivine by weight or volume. In some cases, the mixture may comprise between about 5% and about 30% olivine by weight or volume.\|[0033] Beneficial applications of olivine include, for example, Marsh Restoration, Coastal Engineering/Hazard Mitigation, and CO2 Capture. As described above, olivine sand can react with water and CO2. CO2 may dissolve in water to form carbonic acid. Olivine dissolution may consume the carbonic acid to yield soluble bicarbonate ion (baking soda). This can: Lower atmospheric CO2, Neutralize ocean acidification, and Support the growth of calcifying organisms (Corals, etc).\|[0034] In some cases, olivine sand may be provided to municipalities to augment the sediment used in beach nourishment projects. As the sand weathers, it captures carbon. The sand and its placement are paid for by carbon credits. Therefore, the greater the percentage of olivine sand mixed into the native sand, the cheaper the beach nourishment project. A 10% mix would mean a -10% decrease in sand cost. Through the use of olivine sand, beach nourishment can play a critical role in reversing climate change and ocean acidification if the right mix of native and olivine sand is used. At scale, over a billion tons of CO2 could be removed from the atmosphere every year.\|[0035] Using wave action to break down the olivine is critical to the life cycle. Past analyses have shown that grinding the olivine down to <100µm size is highly energy-intensive. However, grinding the olivine down to >300µm gravel requires far less energy. Using the natural, free energy of water movement to break the olivine down further reduces the milling and grinding energy to a small proportion of the total.\|[0036] Co-Benefits of the methods described herein include, for example: reduction in Ocean Acidification (OA). Ocean acidification has been shown to damage marine ecosystems. Olivine increases local pH levels, potentially mitigating the adverse effects of OA on marine ecosystems. This could potentially improve aquaculture and fishery yields, bolstering local economies at deployment sites as well as reversing damage to marine ecosystems. FIG. 7 illustrates an example of how the oceans can be used for natural carbon storage. Excess CO2 emissions may increase ocean acidity. The systems and methods of the present disclosure may be implemented to reduce acidity and help the oceans safely store more CO2 as bicarbonate.\|[0037] Co-Benefits of the methods described herein may also include, for example: support for diatom growth. Diatoms, marine photosynthetic microalgae, are a cornerstone of marine food webs and capture CO2 through photosynthesis, creating 40% of oxygen on Earth. Diatom abundance has decreased as CO2 has risen, partly due to decreasing concentrations of silicate in the ocean due to damming of rivers limiting sediment flow. Since olivine is primarily magnesium silicate, the increase in silicate concentrations from olivine dissolution may lead to diatom growth. Increases in diatoms would increase the health of marine ecosystems and support photosynthetic carbon capture. Other co-benefits can include, for example, supporting coastal communities facing enhanced coastal erosion and sea level rise by supplying a low-cost source of sediment (which may be paid for using carbon credits).\|Mechanics of Weathering\|[0038] In some cases, grain-on-grain collisions may rapidly break down the olivine. Olivine grains may be reduced in size due to mechanical activation. In some cases, the motion of the water in which the olivine is provided may cause surface abrasions. In some cases, the surface of the olivine grains may be mechanically activated to enable and/or enhance CO2 uptake and de-acidification.\|Sensors\|[0039] In some cases, one or more sensors may be used to track, monitor, and quantify olivine dissolution, CO2 uptake, and ocean de-acidification. The measurements obtained using the sensors may be used to adjust the preparation or processing of the olivine, the optimal properties of the olivine, the location in which the olivine is introduced, the rate at which the olivine is introduced, a method by which the olivine is distributed, or a configuration/form in which the olivine is distributed.\|[0040] In some cases, the one or more sensors may be used to monitor and track: Olivine Dissolution Rates (Porewater Geochemistry, Benthic Flux Measurements), Impacts on Water Chemistry, Ecological Response, Fate, Transport and Bioaccumulation of Cr and Ni, and/or Formation of Secondary Weathering Products (Chrysotile, Carbonates, Clays). In some cases, an isotopic tracer along with [Si] and [ALK] measurements may be used to track olivine dissolution and simultaneous precipitation of secondary clays and carbonate phases. The sensors may also be used to track olivine grains over time [ie physical tracking of olivine using dyes / tracers, etc.].\|Reaction-Transport Modeling\|[0041] In some cases, simulation models may be used to optimize the preparation or processing of the olivine, the properties of the olivine, the location in which the olivine is introduced, the rate at which the olivine is introduced, a method by which the olivine is distributed, or a configuration/form in which the olivine is distributed. The models may be configured to simulate sediment porewater profiles, Water column and Porewater Chemistry (e.g., pCO2, DIC, pH, DO, TA, Nutrients, Metals, DOC), solid-phase chemistry and benthic fluxes, Secondary Clay Mineralogy, and Cr and Ni speciation and cycling. In some cases, the models may be used for simulation of the effects of spreading layers of olivine sand of varying thicknesses on a target beach sediment with one or more known biological, chemical, or ecological properties or characteristics.\|[0042] In some cases, the models may be used simulate or predict Olivine Dissolution Rates, study the impacts of Temperature of Olivine Dissolution & Respiration, track impacts on seawater pH, track Air-Sea Water Gas CO2 Fluxes, monitor and evaluate fate and transport of Cr and Ni, assess the impacts on benthic invertebrates/meiofauna, track sediment characteristics (e.g., changes in mineralogy, formation of secondary carbonate/clays), monitor the impacts of Meteorology and Hydrology (e.g., temperature, wind speed/direction, precipitation, salinity, turbidity, current), or simulate Physical Sediment Transport and/or Olivine Redistribution.\|Method of Removing Atmospheric Carbon\|[0043] [1] In one aspect, the present disclosure provides a method for removing atmospheric carbon using olivine dissolution technologies. The method may be implemented using natural wave energy (i.e., in situ coastal enhanced weathering (CEW)) and/or applied energy (i.e., closed-system artificial weathering of olivine in a man-made reactor or a sand pit resulting from coastal nourishment projects or dredging).\|Bioreactor\|[0044] In another aspect, the present disclosure provides systems and methods to accelerate olivine dissolution reactions in a bioreactor. The bioreactor may comprise one or more internal chambers for housing or storing olivine for any amount of time. The bioreactor may comprise one or more openings or inlets for receiving olivine. The olivine may comprise pure olivine or a mixture of olivine and sand or other elements or materials. The olivine may be unprocessed. Alternatively, the olivine may be processed or pre-processed (e.g., by grinding).\|[0045] In some cases, the bioreactor may comprise one or more mechanical components for mechanical weathering of the olivine. The mechanical weather may cause grain-on-grain collisions that may rapidly break down the olivine. Olivine grains may be reduced in size due to mechanical activation. In some cases, the bioreactor may be in fluid communication with water. In some cases, the bioreactor may comprise an internal chamber for housing the water and/or the olivine. The motion of the water in which the olivine is introduced may cause surface abrasions. In some cases, the surface of the olivine grains may be mechanically activated to enable and/or enhance CO2 uptake and ocean de-acidification.\|[0046] In some cases, the mechanical components may comprise one or more gears or actuators for inducing a motion that cause mechanical weathering of the olivine. The motion may be a linear motion, or a rotational motion, or any combination thereof.\|[0047] In some cases, the bioreactor may comprise a chamber for housing one or more microbial products or other biological mediators and/or enzymatic accelerants that can help to further break down the olivine. The chamber housing the microbial products may be in fluid communication with (i) the chamber housing the olivine, (ii) the chamber that is in fluid communication with the ocean water, or both (i) and (ii).\|[0048] FIG. 8 schematically illustrates an example of a bioreactor 800. The bioreactor 800 may be configured to receive olivine, which olivine may or may not be pre-processed (e.g., by grinding or crushing). The olivine may be stored within a first chamber 810 of the bioreactor 800 for further processing. In some cases, the bioreactor 800 may comprise a second chamber 820 configured to house one or more microbial products or other biological mediators and/or enzymatic accelerants that can help to further break down the olivine. In some cases, the bioreactor 800 may comprise a third chamber 830. The third chamber 830 may comprise a reaction chamber in fluid communication with the first chamber 810 and the second chamber 820. The third chamber 830 may be used to break down the olivine using the microbial products or other biological mediators and/or enzymatic accelerants. Once broken down, the processed olivine may be provided to a target region external to the bioreactor 800 to facilitate CO2 capture and sequestration.\|Microbes\|[0049] [2] In another aspect, the present disclosure provides a method for enhanced dissolution of olivine through (1) microbial products or other biological mediators and (2) enzymatic accelerants. The method may comprise enhancing dissolution of olivine in an olivine reactor or sand pit resulting from coastal nourishment projects or dredging through: microbial products or other biological mediators; and enzymatic accelerants.\|[0050] In another aspect, the present disclosure provides systems and methods for olivine dissolution by microorganisms, biological organisms, and/or biological mechanisms. The dissolution of olivine in water may consume protons and increase alkalinity, thereby removing dissolved aqueous CO2. This aqueous CO2 removal may induce additional CO2 to be taken up from the atmosphere and subsequently converted to bicarbonate, carbonate, and/or solid-phase carbonate minerals, thereby sequestering carbon for long time periods [1]. Scaling and accelerating this process has the potential to mitigate climate change and ocean acidification.\|[0051] In some cases, the reactors disclosed herein may be designed to grow particular microbial strains in an aqueous medium in order to induce metabolic states that can accelerate olivine dissolution. In circum-neutral pH naturally oxygenated waters, ferric iron (Fe2+) contained within olivine may be rapidly oxidized to ferrous iron (Fe3+) by oxygen even in the absence of microbial activity [2]. This oxidized iron can form a surface layer of Fe-oxyhydroxides on the mineral surface of olivine which can shield portions of its total surface area from contact with solution [3]. These Fe-oxyhydroxide surface coatings can, in some cases, impede olivine dissolution [4].\|[0052] For the vast majority of organisms, Fe is a required nutrient and a key component of many cellular proteins. However, most Fe in naturally oxygenated waters at circum-neutral pH is insoluble and typically complexed to particles. Certain microorganisms can produce organic compounds known as siderophores to mobilize and acquire insoluble iron on mineral surfaces [2], which can concurrently increase olivine mineral dissolution rates [3]. However, the production of siderophores may be regulated by Fe availability to the cells. As more Fe is acquired by the cells (i.e. the less iron-limited they are), siderophore production may decrease, which may slow dissolution rates. Hence, in order to sustain and scale siderophore production over extended time periods in large reactors, numerous interacting factors may be optimized:\| 1. The most optimized biological strains (these may be identified through a series of experiments, and in some cases, custom strains may be generated either through directed evolution or genetic editing).\| 2. The optimal ratios of microbial to siderophore concentrations given certain growth conditions.\| 3. Olivine dissolution optimization as a function of particle size/surface area and flow rate from biomass generation.\| 4. Optimized long-term growth conditions for sustained siderophore production.\| 5. Optimized reactor design series including appropriate materials to avoid silicate and trace metal contamination.\| 6. Development of mathematical model to optimize siderophore production yield, biomass generation, and olivine dissolution.\| 7. Development of appropriate parameters to track to feed into the model.\| 8. Development of any treatment of seawater effluent prior to returning to the ocean.\| 9. Development of a model that calculates CO2 sequestration from the addition of alkalinized seawater to the local ocean region.\|System Design\|[0053] Referring to FIG. 11, the illustrated reactor may be configured to intake seawater that may be mixed with olivine and microbial biomass to generate alkalinity. Depending on the source, seawater may have to be pretreated prior to reacting with olivine. This reaction may also result in trace metals, microbial biomass, and other reaction products mixing in with the seawater medium. In order to sequester carbon at scale, this alkaline seawater may be returned to the ocean to induce atmospheric CO2 uptake. Importantly, the return of this seawater containing the certain constituents must meet local regulations. Another microbially-mediated treatment process that returns effluent to the environment may involve anaerobic digestion. This may be a good reference to understand regulations for effluent from microbial processes.\|[0054] In some cases, the reactor may comprise a first chamber for biomass generation (e.g., continuous, semi-continuous, membrane bioreactor), a second chamber for olivine dissolution (e.g., to optimize particle size and flow/recycle biomass), and a third chamber for biomass/suspended olivine separation (and for biomass return to the first chamber). In some cases, sea water based growth media may flow into and/or out of the first chamber. In some cases, CO2 from biomass growth may be provided to the second chamber. The second chamber may also receive biomass with siderophores from the first chamber. The second chamber may provide, in some cases, a recirculation loop for the biomass. The second chamber may be configured to provide the biomass without the siderophores to the third chamber. In some cases, the third chamber may be configured to return biomass to the first chamber. In some cases, the third chamber may be configured to provide the olivine and/or the biomass to seawater.\|[0055] The present disclosure effectively provides methods and designs for sustained microbial growth and siderophore production for olivine dissolution over long time periods. Current methods are unable to accelerate olivine dissolution with microbes for reaction volumes exceeding a few hundred milliliters, unlike the systems and methods disclosed herein. The presently disclosed systems and methods have been developed with the specific engineering and regulatory requirements needed to build large-scale, flow-through reactors with seawater that will then be returned to the local environment. The present disclosure effectively provides systems and methods for optimizing (1) strain selection for olivine dissolution, (2) grain size, (3) culturing conditions with natural seawater, and (4) the materials for the growth chamber.\|Optimizing Olivine\|[0056] [3] In another aspect, the present disclosure provides systems and methods for optimizing olivine for use in the field. Such optimization may comprise, for example, determining the optimal grain size distribution of olivine sand for use in carbon capture (covers combinations of grain size, color, blends, includes modeling grain size for specific sites); and physically and/or chemically processing the olivine (e.g., using machinery) to prepare one or more batches of carbon negative sand suitable for beach nourishment.\|Preparing Olivine\|[0057] [4] In another aspect, the present disclosure provides systems and methods for preparing olivine grains for optimal dissolution. The olivine grains may be part of a source material comprising olivine sand or a mixture comprising olivine sand and local sand.\|[0058] In some cases, the method may comprise crushing raw olivine to yield an optimal grain size and aggregating raw or crushed olivine into pellets. Such processing of the olivine may enhance dissolution of olivine, thereby accelerating the carbon capture process. In some cases, the method may further comprise selecting, milling, and/or matching olivine sand to native sediment for the purpose of coastal protection, beach nourishment and carbon capture.\|[0059] In another aspect, the present disclosure provides carbon-negative sand and processes for producing the same. The carbon-negative sand may comprise specially selected, prepared, and blended mineral particles which [1] are suitable to mitigate coastal erosion along coasts [2] react with carbon dioxide (CO2) and/or dissolved carbonic acid [H2CO3] to produce bicarbonate [HCO3-], [CO32-] ions, and/or solid-phase carbonate minerals [Ca, Mg]CO3, thus [3] simultaneously mitigating the impacts of climate change, ocean acidification, and coastal erosion.\|[0060] In order to be suitable for use in coastal erosion, beach nourishment, and marsh restoration projects, [4] manufactured carbon-negative sand and blends thereof should closely match the texture, grain size distribution, and color of native sediment. Thus, the processes for preparing carbon negative sand may be tailored such that the carbon-negative sand and blends thereof produce and achieve these specific pre-determined properties.\|[0061] In order to mitigate the impacts of carbon dioxide (ie. be "carbon negative"), [5] carbon negative sand may be manufactured from a mafic or ultramafic inorganic mineral or rock (typically naturally occurring olivine, basalt, serpentinite, brucite, wollastonite, or industrial-produced mineralequivalents such as slag). These minerals [6] may react with water and carbon dioxide and/or carbonic acid to produce bicarbonate ion as a reaction product, thereby decreasing the acidity of the surrounding fluid and converting the harmful carbon dioxide or carbonic acid into environmentally beneficial bicarbonate or carbonate ion. An example describing the reaction of forsterite olivine (Mg2SiO4) is provided below, although other minerals and rocks described in this disclosure result in equivalent reactions converting carbonic acid to bicarbonate ion:\| CO2 + H2O → H2CO3\| Mg2SiO4 + 4 H2CO3 → 2 Mg2+ + 4 HCO3- + H4SiO4\|[0062] In order to simultaneously achieve the engineering requirements of sand and sediment for coastal engineering, while preserving the chemical reactivity with carbon dioxide described above, [7] it may be necessary to prepare specially prepare the reactive mineral components and then blend these reactive components in specifically determined ratios with inert native or allochthonous sand and sediment to achieve the desired chemical, engineering, and aesthetic properties. This process is described in greater detail below:\|[0063] The process for preparing the CO2 - reactive component of carbon negative sand begins with a feedstock of mafic or ultramafic rocks, minerals, or their industrially produced equivalents. A list of potential feedstocks is provided in Table 1.\|[0064] Table 1. Potential feedstock materials for the production of the CO2 - reactive component of carbon negative sand.\|Naturally Occurring Rocks: Peridotite, Dunite, Harzburgite, Lherzolite, Basalt, Gabbro, Komatiite, SerpentineNaturally Occurring Minerals: Olivine, Forsterite, Fayalite, Enstatite, Pyroxene, Serpentine, BruciteIndustrial Byproducts: Blast-furnace Slag, Steel-furnace Slag, Basic-oxygen-furnace Slag, Electric-arc-furnace Slag, Ladle Slag.\|[0065] The preparation of the CO2 - reactive components of carbon negative sand may proceed via two critical steps:\| (1) The feedstock may be crushed and/or milled to increase the reactive surface area of the feedstock and provide fresh reactive surfaces for the reaction with carbon dioxide. Because the reaction occurs only on the surfaces of the grains and within microcracks created by the crushing/milling process, it is essential to increase the available reaction surface area to the maximum extent possible in order to maximize the material reactivity.\| (2) The crushed and milled material may then be size sorted using sieves, gravity separation, air classifiers, to provide a final product with a mean grain size and overall grain size distribution which meets the engineering specifications of the coastal engineering project. In some cases, this process may be designed to exclude excessive fine-grained material and/or coarser particles, to produce an intermediate grain-size material which closely matches the size distribution of the native sediment in the geographic region receiving the carbon negative sand. As an alternative to preparing batches of CO2 - reactive components individually, it is also possible to presort the material into various predetermined size ranges and then select and/or blend from these preclassified separates to achieve an overall blend suitable for use in a specific project.\|In most cases or all cases, the CO2 - reactive component may be further modified via mixing non-reactive sediment in order to achieve a combination of texture, color, and density, and engineering properties suitable for use in coastal engineering products. To achieve this, a third step may be required:\| (3) The CO2-reactive mineral component may be blended with one or more chemicallyinert sand and sediment materials to achieve a predetermined ratio providing the specified properties. A list of common non-reactive feedstocks is provided in Table 2. Blends consisting of 1-50% reactive component may be most common, but other variations of this invention, higher or lower fractions of the reactive component may be used.\|Table 2. Potential feedstock materials for the non-reactive component of carbon-negative sand.Naturally Occurring Native Sediment at the Project Site: May include native sand, silt, clay, organic matter and gravelNaturally Occurring Rocks/Sediment: Silicate Beach Sand, Carbonate Beach Sand, Dredged Sediment, Crushed Sandstone, Crushed Limestone, Carbonate OoidsNaturally Occurring Minerals: Quartz, Feldspar, Aragonite, Calcite, Garnet, Magnetite, Hematite, Limonite, Ilmenite, Smectite, Chlorite, Biotite, Muscovite, Rutile, Zircon and Monazite\|[0066] The goal of blending the reactive- and non-reactive sediment components is to achieve a final bulk product meeting various regulatory, aesthetic and engineering requires including color, texture, grain size, density, cohesion, hardness, etc. To realize a blended mixture between the reactive and non-reactive components of the carbon-negative sand mixture, the individual components may either be brought together in advance, or in alternate embodiments, separately conveyed or placed onto the project site in such a manner to realize an appropriate mixture over the duration of the project (ie. mixing between components occurs via the physical motion of sediment driven by conveyors, heavy equipment, and/or waves and tides).\|[0067] Although enhanced silicate weathering may be implemented in some instances, none of the prior work has [8] recognized and provided methods for the manufacture of engineered carbon-negative materials with specific suitable colors, grainsize, density, and reactivity required to meet specific regulatory, aesthetic, and engineering requirement for coastal engineering. Moreover, [9] prior work has completely neglected the engineering of these specific attributes in order to create safe and successful materials for coastal engineering applications. [10] No existing material used in present coastal engineering applications provides additional public and ecological benefits due to CO2 capture, alkalinity generation, and the mitigation of ocean acidification. Likewise, [11] no prior approaches have realized the simultaneous benefits derived from manufacturing carbon-negative materials which are suitable for coastal engineering, thus providing a dual benefit of mitigating coastal erosion and sea level rise.\|Carbon Credits\|[0068] [5] In another aspect, the present disclosure provides systems and methods for measuring, recording and verifying (MRV) carbon removal as well as ecological effects of olivine sand in carbon removal over large coastal areas. Such measurements, recording, and verification of carbon removal may be performed using one or more remote sensors, protocols for the use of such sensors (benthic flux chambers), and algorithms to interpret the data obtained and derived from the sensor readings. The presently disclosed systems may be used to prove the dissolution of olivine and the subsequent capture of CO2 based on the dissolution of the olivine. In some cases, the systems and methods disclosed herein may be implemented to predict dissolution (e.g., by utilizing one or more models for simulating or predicting olivine dissolution at a target site).\|[0069] The present disclosure also provides software configured to calculate CO2 consumption and to measure/record/verify carbon removal. The software may be configured to determine CO2 consumption and/or carbon removal based on one or more sensor readings and/or one or more input parameters. The one or more input parameters may relate to, for example, the physical or chemical properties of the olivine used, the ratio of olivine to sand, the location in which the olivine is distributed, an amount of olivine distributed to a target site, or the manner/configuration in which the olivine is distributed (e.g., method of distribution, form of distribution, or spatial characteristics of the distribution). In some cases, the sensor readings may comprise measurements of alkalinity, pCO2, pH, and/or water temperature.\|[0070] In one aspect, the present disclosure provides methods and protocols for measuring, recording, and verifying (MRV) carbon removal (e.g., by way of coastal carbon capture using olivine). Referring to FIG. 12, the protocols may be submitted to independent, third-party entities (e.g., academics, institutions, etc.) for validation. Once validated, the protocols may be implemented by an individual or an entity. Additional third-party entities may ensure and confirm compliance. The individuals or entities implementing the MRV protocols may then submit the third-party verified, compliant methodologies to a carbon credit verifier, and an offset or a credit may be issued on a registry for sale in domestic and/or international markets.\|[0071] FIGs. 13 - 14 and FIG. 37 show a reaction representing the chemical mechanism by which coastal carbon capture can occur when olivine is introduced to a target site (e.g., by adding olivine sand to beaches and mixing the olivine sand with the native beach sand). For every 1 mol of olivine (which olivine may comprise or exhibit any of the physical or chemical properties or compositions described herein), 4 mols of carbon dioxide may be consumed or captured, and 4 mols of an alkaline material (bicarbonate or HCO3-) may be generated.\|[0072] FIGs. 15 - 20 show an environment comprising a first layer comprising seawater and a second layer comprising sediment and pore water. The sediment and pore water may span a dimension of about 10 centimeters (cm) or about 4 inches (in). The reactions shown in and described in relation to FIGs. 13 - 14 and FIG. 37 may drive the capture of carbon dioxide (e.g., CO2 in the atmosphere or in the seawater) and the release of magnesium, bicarbonate, and silicic acid. The rate of the overall reaction may be determined based on the fluxes associated with CO2 capture and the subsequent release of magnesium, bicarbonate, and silicic acid.\|[0073] In some non-limiting embodiments, one or more stirrers may be used to facilitate the carbon capture process (e.g., by physically mixing the seawater containing olivine sediments with the medium comprising the carbon dioxide). The medium may comprise a liquid medium (e.g., seawater) or a gaseous medium (e.g., air comprising atmospheric carbon dioxide). In some non-limiting embodiments, one or more valves may be used to control and regulate an outflow of any products of the reaction (e.g., the magnesium, bicarbonate, and/or silicic acid).\|[0074] FIG. 21A illustrates a plot of a change in concentration of an alkaline material in a flux chamber as a function of time when the olivine-based carbon capture reactions of the present disclosure are used. The alkalinity of the medium in which the alkaline material is present may gradually increase over time. In some cases, the alkalinity may increase by a factor of 1.1 to 10 or more over a period of 1 to 10 days. As shown in FIG. 21B, the alkalinity flux with olivine increases more rapidly over time than the alkalinity flux at a control site in which olivine is not introduced. The alkalinity flux may correspond to the slope of the lines shown in these plots, and may have units of change in concentration of the alkaline material per unit time.\|[0075] FIG. 22 shows an overview of the porewater method for determining flux of an alkaline material that is produced. The porewater method may be based on Fick's first law of diffusion. The flux of the alkaline material may be determined based on a diffusion coefficient (representing area per unit time) and a dC/dZ value (representing a change in concentration or amount of substance per unit volume, as a function of position or dimensional length). With olivine present in porewater, a larger flux may be observed (steeper slope and bigger flux), whereas when olivine is not present, a smaller flux is observed (shallower slope and smaller flux).\|[0076] FIG. 23 shows a shrinking core model comprising a transformed volume and an untransformed volume of an exemplary olivine particle. The shrinking core model may be represented by X = 1 - [1 - R/(ρ∗d))∗t]^3, where X is the fraction of olivine reacted, R is a function of pH and temperature, p is molar density, d is starting diameter, and t represents time. One assumption for this model is that the particles are a perfect sphere.\|[0077] FIG. 24 shows dissolution rates for olivine having various grain sizes. The fraction of olivine reacted over time may increase more rapidly for olivine particles having smaller grain sizes. For example, for olivine with a 30 micrometer grain size, 10% of the olivine may react within 3 years, 50% of the olivine may react within 18 years, and 90% of the olivine may react within 47 years. In contrast, for olivine with a 64 micrometer grain size, 10% of the olivine may react within 6 years, 50% of the olivine may react within 39 years, and 90% of the olivine may react within 101 years. The rates shown generally correspond to static dissolution rates based on inorganic chemical processes, and may not include acceleration of weathering due to wave energy and biotic processes. The systems and methods of the present disclosure may be implemented to optimize dissolution rates by (1) inducing or imparting wave energy with a specific characteristic (e.g., periodicity, intensity, motion path, etc.) and/or (2) modifying the biotic processes used to enhance olivine dissolution.\|[0078] FIG. 25 shows an exemplary modeling approach for particle distribution. In one step, the modeling approach may comprise simulating grains to match a desired particle size distribution. The modeling approach may further comprise shrinking each particle over a time period (e.g., to simulate dissolution or erosion of one or more portions or layers of each particle), and thereafter summing the total mass of the particles and/or the total amount dissolved or eroded at various time points in order to determine the fraction of mass remaining as a function of time.\|[0079] FIG. 26 shows dissolution rates for different mixtures of olivine having different mean grain sizes. In general, olivine mixtures with smaller mean grain sizes may have a shorter half-life (i.e., a shorter time period for half of the olivine mixture to dissolve under a particular set of conditions).\|[0080] FIG. 27 shows the impact of temperature and pH on half-life. In some cases, the half-life for olivine dissolution may decrease as temperature increases. In some cases, the half-life for olivine dissolution may increase as pH increases. In some embodiments, the systems and methods disclosed herein may be implemented to optimize temperatures and pHs for dissolution environments to shorten the half-life for olivine dissolution. In other embodiments, the systems and methods disclosed herein may be implemented to identify candidate locations with optimal temperatures and pHs for olivine dissolution environments to shorten the half-life for olivine dissolution.\|[0081] The systems and methods disclosed herein may be configured or implemented to overcome challenges relating to spatial and temporal heterogeneity, low signal/noise ratios due to slow dissolution of olivine, and variation in secondary mineral product generation. The systems and methods disclosed herein may also help to overcome verification challenges such as, for example, objective criteria for acceptance and verification of carbon credit sales, and how to influence such criteria to adapt them to coastal weathering processes.\|[0082] The present disclosure provides methods for performing MRV (i.e., the measurement, recording, and verification) of carbon capture and/or olivine dissolution. In some cases, the methods may comprise establishing a treatment site and a reference or baseline site. The methods may further comprise measuring alkalinity fluxes and/or other parameters at a network of discrete locations. In some cases, this may be repeated over time as olivine dissolves over a series of time points. The methods may further comprise interpolating in time and space to determine an overall dissolution rate across an area or a volume of the site. In some cases, the overall dissolution rate across the site may be determined in part using a numerical reaction transport model that provides a fit to the measured data.\|[0083] FIG. 28 shows examples of temporal factors and spatial factors that can vary for coastal ecosystems, many of which are extremely dynamic. Temporal factors may include, for example, diurnal factors (i.e., day/night variations), tides, seasonality, temperature, weather, and/or waves. Spatial factors may include, for example, position and hydrodynamics, depth, tides, sediment type, grain size, sediment organic carbon content, and/or bottom cover (e.g., sea grass, rocks, coral, etc.).\|[0084] In some cases, the methods disclosed herein may comprise assessing or evaluating temporal heterogeneity by measuring depth, temperature, salinity, pH, turbidity, chlorophyll concentrations, and/or dissolved oxygen concentrations over time. FIG. 29 shows plots of temporal heterogeneity of various characteristics for a target site, including depth, salinity, turbidity, temperature, dissolved, oxygen, and pH. In some cases, the target site for olivine distribution and dissolution may be chosen based on temporal heterogeneity relative to other candidate or baseline/reference sites.\|[0085] As shown in FIGs. 30 - 32, in some cases, the methods disclosed herein may comprise calculating alkalinity fluxes and measuring dissolution rates of olivine to secure carbon credits. Alkalinity fluxes induced by olivine may be determined by discerning changes in alkalinity fluxes due to olivine from other natural background fluxes. In some cases, other fluxes attributable to olivine, such as dissolved inorganic carbon (DIC) fluxes and fluxes of pCO2, may be determined based on a comparison of measured fluxes to natural background fluxes. The fluxes attributable to olivine dissolution and/or the natural background fluxes may be space and time dependent. Such variations over space and time may be simulated, modeled, tracked, and/or measured to ensure accurate calculation of fluxes attributable to olivine, as opposed to natural background fluxes.\|[0086] In another aspect, the present disclosure provides various methods for accounting for heterogeneity for MRV. FIG. 33 shows a summary of the MRV approaches described below at different scales of cost and complexity.\|[0087] Approach 1 - In some cases, the methods may involve using the shrinking core model described elsewhere herein for an approximate rate of dissolution. The dissolution rate and CO2/olivine ratio may be assumed or approximated.\|[0088] Approach 2 - Alternatively, mesocosm experiments may be utilized to determine regional olivine dissolution rates. In cases where olivine is deployed in a target site (e.g., a mesocosm or the natural environment), olivine tracers may be used to track olivine dissolution in order to model and refine in situ weathering rates. The present disclosure provides systems and methods to track the movement of olivine grains in a target site. The systems and methods of the present disclosure may be implemented to track olivine transport in a target site based on or using, for example, trace metal content, fluorescent dyes, and/or olivine-specific spectral properties. This may be a relatively inexpensive process that can be set up prior to obtaining regulatory permits. Further, this approach may be initially tested using a sealed, recirculating design that is configured to maintain and control spatiotemporal heterogeneity and further allow for temperature and/or lighting control.\|[0089] Approach 3 - In some cases, the mesocosm-based approaches described herein may be augmented with field data (e.g., in situ data obtained manually or automatically using one or more sensors). The data obtained using the one or more sensors (which one or more sensors may comprise any of the sensors described herein or any other sensors for obtaining any of the measurements referred to herein) may provide additional information to better quantify and track spatial and/or temporal variations in environmental conditions or parameters relating to olivine dissolution and coastal carbon capture.\|[0090] Approach 4 - In some cases, a numerical model may be constructed that allows for accurate simulation of spatial and temporal variations in background fluxes and olivine dissolution rates. This can help to correct for time and space dependent variations, and allow for the use of sparse observations or other information or data at discrete points (e.g., points in time and/or points in space) to calibrate, verify, and validate the model. The model may be built and implemented for one or more a priori simulations.\|[0091] In cases where olivine is deployed in the natural environment, olivine tracers may be used to track olivine dissolution in order to estimate, predict, model, and refine in situ weathering rates. The present disclosure provides systems and methods for tracking the movement or transport of olivine grains in the natural environment (e.g., in a target site in which the olivine is provided or introduced). The systems and methods of the present disclosure may be implemented to track olivine transport based on or using, for example, trace metal content, fluorescent dyes, and/or olivine-specific spectral properties. The trace metal content, the movement or dispersion of fluorescent dyes, and/or the olivine-specific spectral properties may be detected and tracked using any of the sensors described herein.\|[0092] FIG. 34 illustrates various examples of reaction-transport modeling studies that may be used to simulate sediment porewater profiles, solid-phase chemistry, and benthic fluxes. The simulations and studies may be tailored to project requirements, and can take into account secondary clay mineralogy and Cr and Ni speciation and cycling. The plots shown in FIG. 34 illustrate an exemplary numerical simulation of alkalinity profile and the effects of spreading a 2 centimeter (cm) thick layer of pure olivine sand on a beach sediment. In some cases, the alkalinity flux across the sediment-water interface may be monitored by (1) constructing biogeochemical models of olivine dissolution in sediments, (2) validating model performance using field measurements of sediment-water alkalinity flux (and other carbonate parameters), and (3) calculating CO2 capture, storage, or sequestration (by weight or volume) based on the thermodynamics of air-sea CO2 exchange.\|[0093] The systems and methods disclosed herein may be implemented using one or more sensors capable of measuring at optimal spatial and temporal resolutions. The sensors may obviate the need to use traditional, manual geochemical methods, which require labor intensive field sampling and returning of samples to labs for analysis and can involve significant costs. FIG. 35 shows various examples of sensors that can be used for MRV, including sensors configured to measure temperature, salinity, pH, pCO2, DIC, alkalinity, and/or wave impacts on sand. In some cases, a solid state sensor for simultaneous measurement of total alkalinity and pH of seawater (including seawater that does or does not comprise olivine) may be used. In some embodiments, a plurality of sensors for MRV may be deployed on a single system. In other embodiments, a plurality of sensors for MRV may be deployed on multiple separate systems. Additional examples of sensors are shown in FIG. 36, including silicate sensors, alkalinity sensors, CTDO sensors, Cytochips, dissolved inorganic carbon sensors, and nitrate sensors. In some cases, a 29Si isotopic tracer can be used to track olivine dissolution and simultaneous precipitation of secondary clays and carbonate phases. This can allow separation of total and net silicate dissolution.\|[0094] In some cases, the impacts of physical wave-driven weathering on beach sand and olivine dissolution may be measured or simulated. In some cases, this may involve measuring and analyzing 2-phase (i.e., sand-water) flow in the benthic boundary layer of a breaking wave. This may be modeled numerically or physically (e.g., using wave tanks). In some cases, specialized sensors for measuring turbulent energy dissipation (e.g., in a lab or directly on a beach) may be utilized to measure impacts of physical wave-driven weathering.\|[0095] FIG. 38 illustrates an approach to measuring CO2 removal that is enabled by way of the reactions shown in FIG. 37. In some cases, it may not be feasible to monitor the air to sea CO2 flux. Measuring air-sea CO2 fluxes can be challenging because the olivine dissolution signal is strongly muted by dilution with open ocean seawater. For instance, a 1 cm thick layer of olivine dissolving in 5 meters of water in a bay with a 4-hour residence time implies a ~ 1.3 µM increase in water column alkalinity. Measuring net CO2 flux can also be complicated by extreme seasonal and diurnal variations in ΔPCO2air-sea due to changes in local photosynthesis and respiration. Accordingly, in some embodiments, the systems and methods disclosed herein may be implemented to monitor alkalinity flux across the sediment-water interface.\|[0096] In some cases, the models described herein (which models may be generated for specific sites) may undergo validation. Such validation may involve determining olivine abundance, spatial distribution, and dissolution rates at one or more reference points in space or time. In some cases, the reference points may be arranged in a grid pattern. Validation may further involve crossvalidating measured and modeled alkalinity fluxes and olivine dissolution at reference points, and calculating alkalinity flux for a region or a project based on (i) a known mass or volume of olivine deployed and (ii) validated site-specific modeling. The models may be validated using one or more sensor measurements as described elsewhere herein. Once validated, the models may be used to determine or predict olivine dissolution, reaction fluxes, and/or carbon sequestration. In some cases, the models may be updated or refined based on additional sensor measurements captured over a period of time. In some cases, the models may be revalidated based on additional sensor measurements.\|[0097] FIG. 39 illustrates an approach to calculating CO2 sequestration from alkalinity flux based on an expression of how water DIC storage changes as a function of increasing alkalinity. Seawater carbonate chemistry may be controlled by pCO2, pH, DIC, and alkalinity. An isocapnic quotient may be computed based on a change in alkalinity relative to a change in DIC, at fixed conditions for pCO2, temperature, and salinity. In some cases, a 1 micromol increase in alkalinity may yield a 0.78-0.93 micromol DIC increase, which means that for every one ton of forsterite provided to a target site, 0.97 to 1.16 tons of CO2 can be stored as marine DIC.\|[0098] FIG. 40 illustrates a plot showing seawater age and the depth below sea water level of the Atlantic Ocean as a function of latitude (degrees North). CO2 capture via ocean alkalinization requires that the enhanced alkalinity water mass achieves equilibrium with atmospheric pCO2. The precise timescale for pCO2 equilibrium (~ 4 months) and DIC adjustment (~4 years) depends on the Revelle factor (Jones et al. 2014). The time scale for air-sea equilibration is considerably shorter than the time scale for olivine dissolution (~ 10 - 100 year) and approximately similar to the transit time distribution of mixed layer and subtropical mode water (- 10 - 40 years). This means that the surface DIC reservoir can achieve quasi-steady equilibrium throughout equatorial and subtropical regions most suitable for coastal enhanced weather.\|[0099] FIG. 41 illustrates an exemplary CEW life cycle analysis. The life cycle may comprise mining and/or extracting olivine, grinding the olivine to approximately 400 micrometer grain sizes (or less), transporting the olivine to one or more target sites, and spreading the olivine at the target sites. In some cases, the life cycle may be at least about 89% efficient, and can enable sequestration of at least about 5 to 20 times more CO2 than the amount of CO2 emitted during mining, grinding, transportation, and/or spreading of olivine.\|[0100] FIG. 42 illustrates an example of a carbon payback period that can be realized using the methods and systems disclosed herein. In some cases, the break even payback period may occur at approximately 4 years, assuming the following:\| Grainsize: LE45 (d50: 365 µm)\| Temp: 25 °C\| pH: 8\| Embedded emissions: 110 tons CO2 / 1000 tons olivine\| Absorption efficiency: 3 moles ALK / mole olivine\| Dissolution constant: Log(r) = - 8.75 (can vary depending on pH/temp)\|[0101] FIG. 43 illustrates various plots showing exemplary olivine dissolution kinetics for olivine particles having different grain sizes. Dissolution time may decrease as olivine particle sizes decrease. The particle dissolution characteristics may be predicted or simulated using a shrinking core model and one or more laws, equations, or principles governing olivine dissolution rates. In some cases, the shrinking core model may be modified to permit the simulation of dissolution for realistic, commercially-available grain size distributions. The models described herein may be generated by modifying initial diagenesis models to incorporate olivine dissolution kinetics that correspond to the shrinking core model. The models may include and/or account for full carbonate chemistry (e.g., DIC, ALK, pCO2, pH, carbonate precipitation/dissolution) as well as biogeochemical processes (including aerobic and anaerobic respiration, formation of Fe/Mn oxides, pyrite, sulfide oxidation, etc).\|[0102] In some instances, secondary carbonate precipitation as shown in FIG. 44 can impact CO2 capture efficiency. Secondary carbonate precipitation may change the reactions described herein such that for every 1 mol of olivine introduced to a target environment, 2 moles of CO2 are consumed and 0 moles of alkalinity are generated. This can result in a 50% reduction in CO2 capture efficiency. The systems and methods disclosed herein may be implemented to minimize or reduce secondary carbonate precipitation. The rate of carbonate precipitation can be strongly controlled by local variations in geochemistry and biogenic calcification. In some cases, alkalinity export can be the dominant process occurring in sediments, and once mixed into the water column, consumption of alkalinity can be low given the long residence time of DIC and ALK in seawater.\|[0103] In some instances, secondary clay formation as shown in FIG. 45 can impact CO2 capture efficiency. Secondary clay formation may change the reactions described herein such that for every 1 mol of olivine, 8/3 moles of CO2 are consumed and 8/3 moles of alkalinity are generated. This can result in a 33% reduction in CO2 capture efficiency. The systems and methods disclosed herein may be implemented to minimize or reduce such secondary clay formation.\|[0104] In a related aspect, the present disclosure provides systems and methods for simulating a target site or environment. This can allow the study of olivine dissolution rates in a controlled environment, intermediate between lab and field conditions. Such systems and methods may be implemented to determine and/or monitor olivine dissolution rates, porewater geochemistry, or benthic flux measurements, study impacts of temperature on olivine dissolution and respiration, track impacts on seawater pH and other water chemistry, monitor ecological responses and air-sea water gas CO2 fluxes, track the fate, transport, and bioaccumulation of Cr and Ni, track the formation of secondary weathering products (e.g., Chrysotile, Carbonates, Clays), and monitor the impacts of olivine-based CO2 sequestration processes on benthic invertebrates/meiofauna.\|[0105] In some embodiments, the MRV methods and protocols disclosed herein may be adapted or adjusted for different types of olivine or for different target sites for olivine distribution. In such cases, the models used to predict or determine olivine dissolution, reaction fluxes, and/or carbon sequestration may be adjusted based on characteristics of the particular olivine/sand mixture used, the target site, and/or one or more sensor readings or measurements obtained in situ.\|Carbon Removal Prediction\|[0106] [6] In another aspect, the present disclosure provides systems and methods for predicting rates of carbon removal at specific sites. Such predictions may be based on, for example, data corresponding to measurement of changes in alkalinity, pCO2, pH, and/or water temperature. The predictions may be generated using algorithms and software interpreting such data. The algorithms and software may be implemented by way of one or more models that can be generated based on the MRV data obtained using various sensors as described elsewhere herein.\|[0107] In some embodiments, the predicted rates of carbon removal may be used to further optimize the carbon capture process. For instance, the predicted rates may be used to optimize the properties of the olivine sand, the preparation of the olivine sand, and/or the operation or the configuration of the reactor.\|Shipping and Deployment of Olivine\|[0108] [7] In another aspect, the present disclosure provides systems and methods for shipping and deploying olivine. In some cases, the shipping and deployment of olivine may be performed using a device for distributing carbon negative sand in shallow marine environments. The device may be, for example, a spreading device for spreading the olivine in a desired or optimal manner at a target site (e.g., a beach of interest).\|[0109] In some cases, the methods of the present disclosure may comprise determining whether one or more dredging modifications are needed in order to optimally distribute the carbon negative sand. Such determination may be based on one or more sensor readings and/or information about the target site in which the carbon negative sand is to be distributed.\|[0110] In some cases, the olivine may be processed before shipping to facilitate shipping and distribution of the olivine. For instance, the olivine may be modified to enable transportation of ultra-fine material (e.g., for reduction of liquefaction or capsizing risk.\|[0111] In some embodiments, various types and forms of maritime emissions reduction technology (e.g., an on-board olivine reactor driven by ship engine using ballast water) may be implemented. In some cases, bulk carrier direct deployment technology and related modifications (e.g., open sea distribution for in situ CEW) may be utilized. In some cases, grain washing and liquid alkalinity systems may be used for pre-deployment reduction of turbidity. In some cases, global logistics software may be used to mobilize idle maritime assets for carbon removal projects.\|[0112] FIG. 9 schematically illustrates an example of a system that may be used to deploy olivine for coastal nourishment. The system may comprise, for example, a split hulled hopper barge. In some cases, olivine may be mined and milled into carbon negative sand. Thereafter, the olivine may be loaded and shipped on dry bulk carriers to designated ports. The olivine may then be loaded into one or more split hulled hopper barges. In some embodiments, the barges may be linked together and towed to designated deployment sites. Once the barges are positioned at or near the designated deployment sites, the bottom of the barges may be configured to open in order to deploy the olivine. In some cases, sediment transport modeling may be used to predict where the olivine will move and/or in what directions the olivine will disperse.\|[0113] In a further aspect, the present disclosure provides a method and process for conducting carbon neutral and carbon negative dredging operations. The method and process of conducting dredging operations may be either net neutral or net negative with respect to atmospheric greenhouse gas emissions. To achieve this, dredged sediment may be mixed with one or more types of carbon negative sand, as described elsewhere herein. The methods and processes described herein may be adapted for any type of construction activity, including land-based construction activities.\|[0114] The dissolution of carbon negative sand may effect the conversion of gaseous and dissolved carbon dioxide into dissolved bicarbonate and carbonate ions, thereby increasing the capacity of fresh and salt water to store additional carbon in a dissolved state. When present as dissolved bicarbonate and carbonate ions, rather than carbon dioxide, these compounds may no longer contribute to climate change and can act to counter the effect of ocean acidification.\|[0115] In order to reduce, neutralize, or negate carbon dioxide emissions which occur during the combustion of fossil fuels during conventional dredging operations, a predefined ratio of carbon negative sand may be mixed with the dredging spoils in order to [1] result in the net capture of a specified amount of carbon dioxide and [2] ensure that the dredged sediments meet engineering and regulatory requirements for disposal or beneficial reuse. Blends consisting of 1-50% reactive carbon negative component may be most common, but in other variations, higher or lower fractions of the carbon negative component may be used.\|[0116] In order to mix carbon negative sand with dredged materials, several different approaches may be used depending on the type of dredging operation and intended fate of the dredged material. During cutterhead dredging operations, pump-out hopper dredging, and other approaches where dredged material is conveyed via a hydrologic slurry, the carbon negative sand may be directly mixed with the dredge spoils by injecting the carbon negative sand into the slurry pipeline. When using trailing suction hopper dredges, carbon negative sand may be mixed within a sediment hopper or barge prior to discharge. As an alternative, carbon negative sand may be directly placed at the sediment destination in the specified quantity and allowed to mix with the dredge spoils via the action of wind, waves, tides, and currents.\|[0117] Whereas traditional dredging operations consume large quantities of fuel fuels and emit correspondingly large quantities of greenhouse gasses, the method and process described here may allow dredging operations to be conducted in a way that is carbon neutral or even carbon negative over the lifetime of the project. This method and process provides significant advantages, allowing dredging operators to (i) mitigate carbon dioxide emissions on behalf of themselves or their clients, (ii) avoid emissions caps and taxes, and (iii) operate in jurisdictions which impose voluntary or involuntary restrictions on greenhouse gas emissions.\|Carbon-removing marine landfill cap\|[0118] In another aspect, the present disclosure provides carbon-removing marine landfill caps, processes for making the same, and processes for quantifying carbon capture from carbon-removing marine landfill caps. Marine landfills may serve as long-term, seafloor placement areas for unwanted construction debris, dredging materials, and toxic pollutants. Currently, marine landfills are often "capped" with non-toxic clay or sand or other similar materials to prevent contamination of overlying seawater and allow marine life to thrive in previously environmentally damaged areas. By using carbon-removing sand wholly, or as a constituent of, marine landfill caps, these sites can serve as climate change mitigation locales and further encourage the regeneration of environmentally damaged areas through the production of bicarbonate (alkalinity) which offsets ocean acidification and is beneficial for marine life.\|[0119] The process of making and deploying carbon-removing marine landfill cap differs from traditional marine landfill cap because 1) the depth (thickness) of carbon-removing cap sand 2) grain size distribution of carbon-removing cap sand, and 3) possible blend of carbon-removing cap and standard cap must be optimized to 1) prevent release of toxic pollutants and similar while allowing for sufficient permeability so that the carbon-removing sand will capture carbon over time and in particular not saturate sand porewaters such that the carbon removal reaction slows or stops. To achieve these objectives, a carbon-removing marine landfill cap may be deployed wholly as a cap, applied as a single mixture of carbon-removing cap to regular cap sand, or applied in layers where the percentage of carbon-removing cap sand to regular cap sand changes with depth, or the grain size distribution of carbon-removing cap and/or standard cap changes with depth. In all circumstances the carbon capture rates may vary with depth. In some cases, the carbon capture rate may be determined based on analytical measurements and sensor measurements from a particular site, fit to a global model. In some embodiments, the appropriate deployment technique described above may be a function of local wave climate, ecology (bioturbation), seawater temperature, landfill material, and an LCA (life cycle analysis) as the CO2 emitted to deploy the carbon-removing cap must be accounted for to insure the cap is, indeed, carbon-removing.\|Green Hydrogen\|[0120] [8] In another aspect, the present disclosure provides systems and methods for generating and using green hydrogen. As used herein, the term "green hydrogen" may refer to hydrogen that is produced from renewable energy sources and/or low-carbon power sources. The green hydrogen may be used as fuel for fuel cells or internal combustion engines. In some cases, the green hydrogen may be generated based on one or more products or reactants used to drive the CO2 capture and sequestration reactions/methods described elsewhere herein.\|Computer Systems\|[0121] In an aspect, the present disclosure provides computer systems that are programmed or otherwise configured to implement methods of the disclosure, e.g., any of the subject methods for processing and distributing olivine. FIG. 10 shows a computer system 1001 that is programmed or otherwise configured to implement a method for olivine processing and distribution. The computer system 1001 may be configured to, for example, (i) identify a target site, (ii) optimize one or more procedures for processing olivine to yield favorable properties or characteristics for the olivine, based on the target site identified, and (iii) coordinate transportation of the olivine to the target site. The computer system 1001 can be an electronic device of a user or a computer system that is remotely located with respect to the electronic device. The electronic device can be a mobile electronic device.\|[0122] The computer system 1001 may include a central processing unit (CPU, also "processor" and "computer processor" herein) 1005, which can be a single core or multi core processor, or a plurality of processors for parallel processing. The computer system 1001 also includes memory or memory location 1010 (e.g., random-access memory, read-only memory, flash memory), electronic storage unit 1015 (e.g., hard disk), communication interface 1020 (e.g., network adapter) for communicating with one or more other systems, and peripheral devices 1025, such as cache, other memory, data storage and/or electronic display adapters. The memory 1010, storage unit 1015, interface 1020 and peripheral devices 1025 are in communication with the CPU 1005 through a communication bus (solid lines), such as a motherboard. The storage unit 1015 can be a data storage unit (or data repository) for storing data. The computer system 1001 can be operatively coupled to a computer network ("network") 1030 with the aid of the communication interface 1020. The network 1030 can be the Internet, an internet and/or extranet, or an intranet and/or extranet that is in communication with the Internet. The network 1030 in some cases is a telecommunication and/or data network. The network 1030 can include one or more computer servers, which can enable distributed computing, such as cloud computing. The network 1030, in some cases with the aid of the computer system 1001, can implement a peer-to-peer network, which may enable devices coupled to the computer system 1001 to behave as a client or a server.\|[0123] The CPU 1005 can execute a sequence of machine-readable instructions, which can be embodied in a program or software. The instructions may be stored in a memory location, such as the memory 1010. The instructions can be directed to the CPU 1005, which can subsequently program or otherwise configure the CPU 1005 to implement methods of the present disclosure. Examples of operations performed by the CPU 1005 can include fetch, decode, execute, and writeback.\|[0124] The CPU 1005 can be part of a circuit, such as an integrated circuit. One or more other components of the system 1001 can be included in the circuit. In some cases, the circuit is an application specific integrated circuit (ASIC).\|[0125] The storage unit 1015 can store files, such as drivers, libraries and saved programs. The storage unit 1015 can store user data, e.g., user preferences and user programs. The computer system 1001 in some cases can include one or more additional data storage units that are located external to the computer system 1001 (e.g., on a remote server that is in communication with the computer system 1001 through an intranet or the Internet).\|[0126] The computer system 1001 can communicate with one or more remote computer systems through the network 1030. For instance, the computer system 1001 can communicate with a remote computer system of a user (e.g., an end user performing or monitoring the processing and/or the transportation or distribution of the olivine). Examples of remote computer systems include personal computers (e.g., portable PC), slate or tablet PC's (e.g., Apple® iPad, Samsung® Tab), telephones, Smart phones (e.g., Apple® iPhone, Android-enabled device, Blackberry®), or personal digital assistants. The user can access the computer system 1001 via the network 1030.\|[0127] Methods as described herein can be implemented by way of machine (e.g., computer processor) executable code stored on an electronic storage location of the computer system 1001, such as, for example, on the memory 1010 or electronic storage unit 1015. The machine executable or machine readable code can be provided in the form of software. During use, the code can be executed by the processor 1005. In some cases, the code can be retrieved from the storage unit 1015 and stored on the memory 1010 for ready access by the processor 1005. In some situations, the electronic storage unit 1015 can be precluded, and machine-executable instructions are stored on memory 1010.\|[0128] The code can be pre-compiled and configured for use with a machine having a processor adapted to execute the code, or can be compiled during runtime. The code can be supplied in a programming language that can be selected to enable the code to execute in a pre-compiled or ascompiled fashion.\|[0129] Aspects of the systems and methods provided herein, such as the computer system 1001, can be embodied in programming. Various aspects of the technology may be thought of as "products" or "articles of manufacture" typically in the form of machine (or processor) executable code and/or associated data that is carried on or embodied in a type of machine readable medium. Machine-executable code can be stored on an electronic storage unit, such as memory (e.g., read-only memory, random-access memory, flash memory) or a hard disk. "Storage" type media can include any or all of the tangible memory of the computers, processors or the like, or associated modules thereof, such as various semiconductor memories, tape drives, disk drives and the like, which may provide non-transitory storage at any time for the software programming. All or portions of the software may at times be communicated through the Internet or various other telecommunication networks. Such communications, for example, may enable loading of the software from one computer or processor into another, for example, from a management server or host computer into the computer platform of an application server. Thus, another type of media that may bear the software elements includes optical, electrical and electromagnetic waves, such as used across physical interfaces between local devices, through wired and optical landline networks and over various air-links. The physical elements that carry such waves, such as wired or wireless links, optical links or the like, also may be considered as media bearing the software. As used herein, unless restricted to non-transitory, tangible "storage" media, terms such as computer or machine "readable medium" refer to any medium that participates in providing instructions to a processor for execution.\|[0130] Hence, a machine readable medium, such as computer-executable code, may take many forms, including but not limited to, a tangible storage medium, a carrier wave medium or physical transmission medium. Non-volatile storage media including, for example, optical or magnetic disks, or any storage devices in any computer(s) or the like, may be used to implement the databases, etc. shown in the drawings. Volatile storage media include dynamic memory, such as main memory of such a computer platform. Tangible transmission media include coaxial cables; copper wire and fiber optics, including the wires that comprise a bus within a computer system. Carrier-wave transmission media may take the form of electric or electromagnetic signals, or acoustic or light waves such as those generated during radio frequency (RF) and infrared (IR) data communications. Common forms of computer-readable media therefore include for example: a floppy disk, a flexible disk, hard disk, magnetic tape, any other magnetic medium, a CD-ROM, DVD or DVD-ROM, any other optical medium, punch cards paper tape, any other physical storage medium with patterns of holes, a RAM, a ROM, a PROM and EPROM, a FLASH-EPROM, any other memory chip or cartridge, a carrier wave transporting data or instructions, cables or links transporting such a carrier wave, or any other medium from which a computer may read programming code and/or data. Many of these forms of computer readable media may be involved in carrying one or more sequences of one or more instructions to a processor for execution.\|[0131] The computer system 1001 can include or be in communication with an electronic display 1035 that comprises a user interface (UI) 1040 for providing, for example, a portal for a user to monitor the processing and/or the transportation or distribution of the olivine. The portal may be provided through an application programming interface (API). A user or entity can also interact with various elements in the portal via the UI. Examples of UI's include, without limitation, a graphical user interface (GUI) and web-based user interface.\|[0132] Methods and systems of the present disclosure can be implemented by way of one or more algorithms. An algorithm can be implemented by way of software upon execution by the central processing unit 1005. For example, the algorithm may be configured to identify a target site and optimize a procedure for processing the olivine based on the properties or the characteristics of the target site.\|[0133] While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. It is not intended that the invention be limited by the specific examples provided within the specification. While the invention has been described with reference to the aforementioned specification, the descriptions and illustrations of the embodiments herein are not meant to be construed in a limiting sense. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. Furthermore, it shall be understood that all aspects of the invention are not limited to the specific depictions, configurations or relative proportions set forth herein which depend upon a variety of conditions and variables. It should be understood that various alternatives to the embodiments of the invention described herein may be employed in practicing the invention. It is therefore contemplated that the invention shall also cover any such alternatives, modifications, variations or equivalents. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby.	Family Number\|(104628663)\|104628663\|Advantages / Prev. Drawbacks\|(EP4166641 A1)\|The systems and methods of the present disclosure enable the acceleration of Earth's natural carbon removal method of rock weathering, through the extraction, processing (e.g., crushing and/or grinding), and transportation of volcanic mineral olivine to coastlines for dispersal or distribution.\|Independent Claims\|(EP4166641 A1)\| (...) (a) generating one or more models for determining or predicting olivine dissolution, carbon sequestration, or one or more reaction fluxes associated with a dissolution of olivine in a target environment; (...) (d) using the one or more validated and/or updated models to determine or predict (i) olivine dissolution, (ii) carbon sequestration, and (iii) the one or more reaction fluxes in the target environment.\|	Biotechnology	C12M-025/16\|C12M-043/04\|Y02C-020/40		C12M-025/16\|C12M-043/04\|Y02C-020/40	C12M-001/12	C12M-001/12			GB2636851	GB2636851 108540140 WHO=Examiner SELF=N				XP055953515; XP086406848; XP055953378; XP028640436; XP055811339	(EP4166641)\|Applicant references\|-GERRITS RUBEN: "An experimental study of fungal olivine weathering", 1 January 2019 (2019-01-01), XP055953515, Retrieved from the Internet <URL:https://opus4.kobv.de/opus4-bam/files/48825/Dissertation-Ruben%20Gerrits-final.pdf> [retrieved on 20220822], DOI: 10.17169/refubium-2880\|-GERRITS R ET AL: "High-resolution imaging of fungal biofilm-induced olivine weathering", CHEMICAL GEOLOGY, ELSEVIER SCIENCE PUBLISHER B.V., AMSTERDAM, NL, vol. 559, 24 September 2020 (2020-09-24), XP086406848, ISSN: 0009-2541, [retrieved on 20200924], DOI: 10.1016/J.CHEMGEO.2020.119902\|-TORRES MARK A. ET AL: "Microbial Acceleration of Olivine Dissolution via Siderophore Production", PROCEDIA EARTH AND PLANETARY SCIENCE, vol. 10, 1 January 2014 (2014-01-01), AMSTERDAM, NL, pages 118 - 122, XP055953378, ISSN: 1878-5220, Retrieved from the Internet <URL:https://www.researchgate.net/profile/Kenneth-Nealson/publication/265089771_Microbial_Acceleration_of_Olivine_Dissolution_via_Siderophore_Production/links/546caa6b0cf24b753c628dad/Microbial-Acceleration-of-Olivine-Dissolution-via-Siderophore-Production.pdf> DOI: 10.1016/j.proeps.2014.08.041\|-MOROZ LYUBA V ET AL: "Space weathering of silicate regoliths with various FeO contents: New insights from laser irradiation experiments and theoretical spectral simulations", ICARUS, ACADEMIC PRESS, SAN DIEGO, CA, US, vol. 235, 24 March 2014 (2014-03-24), pages 187 - 206, XP028640436, ISSN: 0019-1035, DOI: 10.1016/J.ICARUS.2014.03.021\|-KÖHLER PETER ET AL: "Environmental Research Letters LETTER @BULLET OPEN ACCESS Geoengineering impact of open ocean dissolution of olivine on atmospheric CO 2 , surface ocean pH and marine biology", ENVIRON. RES. LETT, 21 January 2013 (2013-01-21), pages 14009 - 9, XP055811339, Retrieved from the Internet <URL:https://iopscience.iop.org/article/10.1088/1748-9326/8/1/014009/pdf> [retrieved on 20210608]\|	LAPSED	(EP4166641)\|LAPSED	DEAD	(EP4166641)\|DEAD	(EP4166641)\|LEGAL DETAILS FOR EP4166641\|Actual or expected expiration date=2023-10-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-02-17\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP22157366\|Application date=2022-02-17\|Standardized application number=2022EP-0157366\|Event publication date=2023-03-17\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2023-03-17\|Event code=EP/STAAPB\|Event group=Examination events\|The application has been published\|Original code: STAA\|Event publication date=2023-04-19\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP4166641\|Publication stage code=A1\|Publication date=2023-04-19\|Standardized publication number=EP4166641\|Event publication date=2023-04-19\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2024-02-16\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2024-03-20\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2023-10-20	(EP4166641)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP4166641)\|Extension States: ME, BA\|(EP4166641)\|Validation States: MA, MD, TN, KH		https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=VCVyqWEeIcCG2afaYUkNFqCa4vFyxJplNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP0000000010242243&ekey=2092&xpn=EP4166641&kind=A1	https://register.epo.org/application?number=EP22157366	https://permalink.orbit.com/RenderStaticFirstPage?XPN=f6P6m2tQ6MEuw56Xk6cpNXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(EP4166641)\|US	(EP4166641)\|NAME=Project Vesta, PBC 584 Castro St 2054 , CITY=San Francisco, CA 94114 , COUNTRY=US , REG=101937721	(EP4166641)\|GB	(EP4166641)\|NAME=Hamer, Christopher K. Mathys & Squire , CITY=The Shard32 London Bridge StreetLondon SE1 9SG , COUNTRY=GB , REG=100052783	(EP4166641)\|US; US; US; US; US; US; US	(EP4166641)\|NAME=ROMANIELLO, Stephen Justin, CITY=San Francisco, 94114, COUNTRY=US \|NAME=LEY, Brian David, CITY=San Francisco, 94114, COUNTRY=US \|NAME=ANDREWS, Margaret Grace, CITY=San Francisco, 94114, COUNTRY=US \|NAME=WALWORTH, Nathan Gerard, CITY=San Francisco, 94114, COUNTRY=US \|NAME=ISHOEY, Thomas, CITY=San Francisco, 94114, COUNTRY=US \|NAME=GREEN, Tom Coxeter, CITY=San Francisco, 94114, COUNTRY=US \|NAME=MONTSERRAT, Francesc, CITY=San Francisco, 94114, COUNTRY=US	(EP4166641)\|45	3	1					(EP4166641)\|Number of Claims: NCL=10\|Primary examiner: Cubas Alcaraz, Jose\|		(EP4166641)\|ENGLISH (ENG)	(EP4166641)\|Patent	Titre: (EP4166641)\|Systems and methods for processing olivine Résumé: (EP4166641)\|The present disclosure provides a system for processing olivine. The system may comprise a reactor for accelerating olivine weathering. The reactor may comprise one or more chambers for housing one or more microbes, biological mediators, or enzymatic accelerants to facilitate the olivine weathering.	35	Abstract	gpt-4o-mini	yes	The article describes a system for processing olivine to accelerate its weathering, which is directly related to enhanced weathering for CO₂ capture.
41	CN202510926442	US19/420,413\|CN202510926442	US20260104346\|CN120404566\|CN120404566	115489354	US20260104346 A1 2026-04-16 [US20260104346]\|CN120404566 B 2025-09-05 [CN120404566B]\|CN120404566 A 2025-08-01 [CN120404566]	2025-07-07	2025-12-15\|2025-07-07	2026-04-16\|2025-09-05\|2025-08-01	\|(CN120404566B)\|2025-09-05	(US20260104346)\|2045-12-15\|(CN120404566)\|2045-07-07	(US20260104346)\|An Experimental System for Rock Corrosion by Supercritical Carbon Dioxide	(US20260104346)\|The present invention relates to an experimental system and usage method for supercritical carbon dioxide rock corrosion. The experimental system comprises a corrosion vessel for exposing samples to a saturated carbon dioxide aqueous solution. The inside of the corrosion vessel is provided with a heating assembly and a rock sample placement rack. The top of the rock sample placement rack is above the liquid level of saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is submerged in saturated carbon dioxide aqueous solution. The heating assembly is located on the perimeter wall of the corrosion vessel and connected with a controller. The corrosion vessel is connected to a carbon dioxide gas delivery unit and a booster pump assembly connected via a conveying pipe. The present invention enables rocks to corrode in both supercritical and carbon dioxide solutions.	CHINA UNIVERSITY OF MINING & TECHNOLOGY\|SHAOXING UNIVERSITY	(US20260104346)\|Shaoxing University ([CN])\|China University of Mining and Technology ([CN])\|(CN120404566)\|CHINA UNIVERSITY OF MINING & TECHNOLOGY ([CN])\|(CN120404566)\|CHINA UNIVERSITY OF MINING & TECHNOLOGY ([CN])	YANG Shengqi\|LI Yue\|HUANG Yanhua\|YIN Pengfei\|TIAN Wenling\|ZHU Zhennan	(US20260104346)\|YANG Shengqi\|LI Yue\|HUANG Yanhua\|YIN Pengfei\|TIAN Wenling\|ZHU Zhennan	(CN120404566)\|JI LI;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP)\|Reg. Nb: 61223	(US20260104346)\|Accordingly it is of great significance to provide an experimental system to study the corrosion of rock in geological storage environments comprising supercritical carbon dioxide.\|	(US20260104346)\|1. An experimental system for assaying rock corrosion in supercritical carbon dioxide, comprising a corrosion vessel (1), wherein: the corrosion vessel (1) contains saturated carbon dioxide aqueous solution; a top opening of the corrosion vessel (1) is connected with a sealing cover; the corrosion vessel (1) is provided with a heating assembly and contains a rock sample placement rack; a top of the rock sample placement rack is located above the liquid level of the saturated carbon dioxide aqueous solution, and a bottom of the rock sample placement rack is submerged in the saturated carbon dioxide aqueous solution; the heating assembly is arranged on a perimeter wall of the corrosion vessel (1) and connected with a controller (6); the controller (6) regulates the temperature of the heating assembly, and is capable of regulating the temperature of the heating assembly to provide conditions for maintaining a carbon dioxide supercritical state; the corrosion vessel (1) is connected with a carbon dioxide gas conveying unit through a conveying pipe, and the carbon dioxide gas conveying unit comprises: a gas source storage tank (5) configured to supply carbon dioxide gas, wherein the gas source storage tank (5) has a gas outlet; a gas booster pump assembly, configured to provide conditions for maintaining a supercritical state of carbon dioxide, wherein the gas booster pump assembly and the gas outlet are connected through a pipeline, and the gas booster pump assembly is connected to the conveying pipe; the corrosion vessel (1) comprises two independent corrosion chambers, a first corrosion chamber and a second corrosion chamber, and the first corrosion chamber and the second corrosion chamber are both configured to contain saturated carbon dioxide aqueous solution; at least two rock sample placement racks are provided, and each rock sample placement rack is respectively provided in the first corrosion chamber and the second corrosion chamber; the sealing cover includes a first sealing cover (2) and a second sealing cover (101); the first sealing cover (2) is threadedly connected to the top opening of the first corrosion chamber, and the second sealing cover (101) is threadedly connected to the bottom opening of the second corrosion chamber; the delivery pipe includes a first transmission pipe and a second transmission pipe; the first transmission pipe and the second transmission pipe are both connected to the gas booster pump assembly through a pipeline; the first transmission pipe passes through the first sealing cover (2) and is connected to the first corrosion chamber, and the second transmission pipe is connected to the second corrosion chamber.\|	(US20260104346)\|As shown in FIGS. 1 to 8, the present invention provides an experimental system for supercritical carbon dioxide rock corrosion, including a corrosion vessel 1, wherein the corrosion vessel 1 is used to store a saturated carbon dioxide aqueous solution, and the top of the corrosion vessel 1 is open and connected to a sealing cover, and a heating component and a rock sample placement rack are provided inside the corrosion vessel 1, wherein the top of the rock sample placement rack is located above the liquid surface of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is immersed in the saturated carbon dioxide aqueous solution, and the heating component is provided on the peripheral wall of the corrosion vessel 1 and connected to a controller 6, wherein the controller 6 regulates the temperature of the heating component so that the temperature of the heating component after regulation provides a temperature that maintains the supercritical state of carbon dioxide.\|The present invention relates to an experimental system and usage method for supercritical carbon dioxide rock corrosion.\|To address the shortcomings of the prior art, the present invention aims to provide a supercritical CO_2 rock corrosion experimental system and method of use.\|	(US20260104346)\|SUPERCRITICAL CARBON DIOXIDE(100,29)\|EXPERIMENTAL SYSTEM(100,19)\|ASSAYING ROCK CORROSION(100,7)\|STONE CORROSION(100,2)\|CORROSION VESSEL(96,58)\|CORROSION CHAMBER(75,33)\|PLACEMENT RACK(71,16)\|ROCK SAMPLE PLACEMENT RACK(56,4)\|CARBON DIOXIDE SATURATION(48,20)\|TRANSMISSION PIPE(43,12)\|CONVEYING PIPE(42,8)\|AQUEOUS SOLUTION(40,20)\|GAS BOOSTER PUMP(35,32)\|CORROSION VESSEL PERIMETER WALL(34,3)\|ROCK CORROSION(34,1)\|SEALING(32,40)\|ROCK BOTTOM(26,4)\|PIPELINE(25,19)\|PERIMETER WALL(22,3)\|HEATING COMPONENT(21,7)\|CONVEYER PIPE(21,6)\|CORROSION VESSEL PERIPHERAL WALL(21,1)\|TEFLON CLAD WIRE(20,2)\|ROCK(19,18)\|CARBON DIOXIDE GAS(19,17)\|SIGNIFICANCE(19,1)\|DELIVERY PIPE(18,7)\|GAS OUTLET(18,7)\|HEATING TEMPERATURE(18,7)\|CORROSION CHAMBER THREAD(18,3)\|GEOLOGICAL STORAGE ENVIRONMENT(16,7)\|CORROSION VESSEL TOP(16,1)\|MAINTAINING CARBON DIOXIDE(16,1)\|REGULATION(16,1)\|CORROSION(14,10)\|PERIPHERAL WALL(14,1)\|SUPERCRITICAL PHASE(13,3)\|HEATING COMPONENT TEMPERATURE(12,3)\|ANTI CORROSION ALLOY(12,2)\|THREADED INTERFACE(11,2)\|CARBON DIOXIDE(10,17)\|GAS SOURCE STORAGE TANK(10,9)\|PRESSURIZING(10,3)\|CORROSION CHAMBER BOTTOM OPENING(10,2)\|BUFFER VESSEL AIR INLET(9,3)\|CORROSION VESSEL TOP OPENING(9,2)\|SEALING RING(8,16)\|TOP OPENING(8,4)\|ROCK CORROSION EXPERIMENTAL SYSTEM(8,3)\|CORROSION CHAMBER TOP OPENING(8,2)\|GEOLOGICAL EXPLORATION(8,2)\|UPPER SLEEVE(8,2)\|PRESSURIZED CARBON DIOXIDE GAS(7,4)\|BUFFER VESSEL AIR OUTLET(7,3)\|BOTTOM OPENING(7,2)\|ROCK CORROSION SIMULATION EXPERIMENT(7,1)\|GEOLOGICAL SEQUESTRATION ENVIRONMENT(6,1)\|SEALING COVER(5,5)\|ROCK COEXISTENCE(5,1)\|ROCK CORROSION CURING(5,1)\|SIMULTANEOUS CORROSION EXPERIMENT(5,1)\|INLET PIPE(4,7)\|CARBON DIOXIDE GROUNDWATER SOLUTION(4,3)\|LIQUID LEVEL(4,3)\|CORROSION RESISTANT ALLOY(4,2)\|ENTRY PIPE(4,2)\|PRESSURE GAUGE(3,10)\|GAS SOURCE TANK(3,6)\|DRIVE CYLINDER(3,5)\|LIQUID PHASE ENVIRONMENT(3,4)\|TEMPERATURE CONTROLLER(3,4)\|DELIVERY UNIT(3,3)\|OUTLET END(3,3)\|CORROSION PRODUCT(3,2)\|GAS SCREW INTERFACE(3,2)\|MINERAL(3,2)\|ROCK SAMPLE HOLDER(3,2)\|SPECIMEN(3,2)\|CORROSION ASSAY(3,1)\|EXPOSING ROCK(3,1)\|ORDINARY SKILL PERSON(3,1)\|POLYTETRAFLUOROETHYLENE(3,1)\|SEALING MIDDLE(3,1)\|VESSEL CORROSION(3,1)\|\|(CN120404566)\|CARBON DIOXIDE(100,103)\|CONVEYING PIPE(100,20)\|EXPERIMENTAL SYSTEM(100,17)\|CARBON DIOXIDE ROCK CORROSION(100,16)\|STONE CORROSION(100,16)\|CORROSION CHAMBER(88,40)\|CORROSION VESSEL(83,11)\|CORROSION CONTAINER(82,52)\|CORROSION VESSEL PERISPORIUM(72,1)\|GEOLOGICAL SEQUESTRATION ENVIRONMENT(60,1)\|ROCK CORROSION EXPERIMENT(56,3)\|GEOLOGICAL EXPLORATION(43,2)\|ROCK(40,17)\|ROCK SAMPLE PLACING RACK(40,5)\|ROCK BOTTOM SUBMERGENCE(39,1)\|PLACING RACK(38,4)\|CARBON DIOXIDE GROUNDWATER SOLUTION(38,3)\|GAS OUTLET(37,11)\|ROCK SAMPLE RACK(36,2)\|CONVEYER PIPE(35,2)\|GAS BOOSTER PUMP(34,29)\|SUPERCRITICAL CARBON DIOXIDE(34,9)\|EXPERIMENT(34,7)\|CARBONATE ROCK(34,1)\|PIPELINE(33,19)\|COEXISTENCE(32,2)\|SAMPLE PLACEMENT(31,5)\|SEALING(30,33)\|BUFFER CONTAINER(30,21)\|AQUEOUS SOLUTION(30,18)\|MINERAL(30,2)\|CONVEYING GAS(30,1)\|GROUNDWATER SOLUTION(28,1)\|GAS BOOSTER PUMP COMPONENT(27,2)\|BOTTOM SUBMERGENCE(27,1)\|PIPELINE EXTERIOR(27,1)\|RESISTANT CORROSION RESISTANT ALLOY(27,1)\|ROCK SAMPLE PLACING FRAME(26,6)\|CARBON DIOXIDE AQUEOUS SOLUTION(25,18)\|GAS SOURCE TANK(25,2)\|CARBON DIOXIDE GAS CONVEYING(24,1)\|CORROSION CHAMBER BOTTOM(24,1)\|INORGANIC PHASE(24,1)\|HEATING COMPONENT(22,11)\|SEALING COVER(22,8)\|CARBON DIOXIDE GAS(21,13)\|THREADED CONNECTION(21,11)\|CORROSION CONTAINER PERIPHERAL WALL(21,3)\|RACK(21,3)\|POLYTETRAFLUOROETHYLENE COATED WIRE(21,2)\|ROCK CHEMICAL PROPERTY(21,1)\|SEALING LID(20,7)\|GEOLOGICAL STORAGE ENVIRONMENT(20,5)\|ROCK BOTTOM(20,2)\|WATER SOLUTION(20,2)\|CORROSION CHAMBER TOP(20,1)\|CONVEYER(19,2)\|REGULATION(19,2)\|BUFFER VESSEL(19,1)\|SILICATE(18,1)\|CARBON DIOXIDE WATER SOLUTION(17,2)\|UPPER CORROSION CHAMBER(17,2)\|SUPERCRITICAL PHASE(16,4)\|HEATING ELEMENT(15,5)\|DELIVERY PIPE(15,3)\|PERIPHERAL WALL(14,3)\|SUPPLYING CARBON DIOXIDE(14,3)\|CHEMICAL PROPERTY(14,2)\|TRUE RESEARCH DATA(14,1)\|MUTUALLY INDEPENDENT(13,2)\|RESEARCH DATA RELIABILITY(13,1)\|CARBON DIOXIDE SOLUTION(12,5)\|BOOSTED CARBON DIOXIDE(12,3)\|THREADED INTERFACE(12,3)\|GAS INLET(12,1)\|BOOSTING(11,3)\|CORROSION CONTAINER TOP OPENING(11,2)\|SEALING RING(10,16)\|PIPE INTRODUCTION(9,6)\|CHEMICAL ENGINEERING(9,2)\|MATERIALS SCIENCE(9,1)\|ROCK CORROSION SIMULATION EXPERIMENT(9,1)\|HEATING COMPONENT TEMPERATURE(8,4)\|HEATING TEMPERATURE(7,4)\|CARBON DIOXIDE PRESSURE(7,1)\|TEMPERATURE RESISTANT PRESSURE(7,1)\|GAS SOURCE STORAGE TANK(6,9)\|DRIVING CYLINDER(6,5)\|TRANSMISSION PIPE(6,5)\|LIQUID LEVEL(6,4)\|TOP OPENING(6,3)\|ROCK CORROSION MAINTENANCE(6,1)\|AIR SOURCE STORAGE TANK(5,6)\|PRESSURIZED CARBON DIOXIDE(5,4)\|GEOLOGICAL SEALING ENVIRONMENT(5,1)\|MUTUAL INDEPENDENCE CORROSION CHAMBER(5,1)\|PRESSURE GAUGE(4,10)\|LIQUID PHASE ENVIRONMENT(4,4)\|TRANSFER PIPE(4,3)\|CORROSION RESEARCH(4,1)\|POLYTETRAFLUOROETHYLENE COVERED WIRE(4,1)\|SEALED LID CORROSION CHAMBER(4,1)\|\|(CN120404566)\|CARBON DIOXIDE(100,102)\|CORROSION CONTAINER(100,58)\|EXPERIMENTAL SYSTEM(100,17)\|CARBON DIOXIDE ROCK CORROSION(100,16)\|STONE CORROSION(100,16)\|ROCK CORROSION EXPERIMENT(63,4)\|CONVEYING PIPE(59,16)\|CORROSION CHAMBER(57,40)\|GEOLOGICAL SEQUESTRATION ENVIRONMENT(56,1)\|GEOLOGICAL EXPLORATION(40,2)\|ROCK SAMPLE PLACING RACK(37,5)\|SUPERCRITICAL CARBON DIOXIDE(36,10)\|PLACING RACK(36,4)\|CARBON DIOXIDE GROUNDWATER SOLUTION(36,3)\|GAS OUTLET(35,11)\|ROCK SAMPLE RACK(34,2)\|ROCK(33,16)\|CONVEYER PIPE(33,2)\|PIPELINE(32,20)\|EXPERIMENT(32,7)\|CARBONATE ROCK(32,1)\|GAS BOOSTER PUMP(30,29)\|COEXISTENCE(30,2)\|SAMPLE PLACEMENT(29,5)\|BUFFER CONTAINER(28,21)\|MINERAL(28,2)\|GROUNDWATER SOLUTION(27,1)\|PERISPORIUM(27,1)\|RESISTANT CORROSION RESISTANT ALLOY(26,1)\|GAS BOOSTER PUMP COMPONENT(25,2)\|GAS SOURCE TANK(24,2)\|INORGANIC PHASE(22,1)\|HEATING COMPONENT(21,11)\|CORROSION CONTAINER PERIPHERAL WALL(20,3)\|ROCK CHEMICAL PROPERTY(20,1)\|SEALING LID(19,7)\|GEOLOGICAL STORAGE ENVIRONMENT(19,5)\|ROCK BOTTOM(19,2)\|WATER SOLUTION(19,2)\|AQUEOUS SOLUTION(18,16)\|REGULATION(18,2)\|BUFFER VESSEL(18,1)\|CORROSION VESSEL(17,5)\|SILICATE(17,1)\|CARBON DIOXIDE GAS(16,12)\|CARBON DIOXIDE WATER SOLUTION(16,2)\|CARBON DIOXIDE AQUEOUS SOLUTION(15,16)\|THREADED CONNECTION(15,11)\|SUPERCRITICAL PHASE(15,4)\|SEALING COVER(14,7)\|HEATING ELEMENT(14,5)\|ROCK SAMPLE PLACING FRAME(14,5)\|DELIVERY PIPE(14,3)\|PERIPHERAL WALL(14,3)\|GAS DELIVERY UNIT(14,2)\|SUPPLYING CARBON DIOXIDE(13,3)\|CHEMICAL PROPERTY(13,2)\|RESEARCH DATA RELIABILITY(13,1)\|TRUE RESEARCH DATA(13,1)\|CARBON DIOXIDE SOLUTION(12,5)\|BOOSTED CARBON DIOXIDE(12,3)\|THREADED INTERFACE(12,3)\|GAS INLET(12,1)\|BOOSTING(10,3)\|CORROSION CONTAINER TOP OPENING(10,2)\|SEALING RING(9,16)\|UPPER CORROSION CHAMBER(9,2)\|PIPE INTRODUCTION(8,6)\|HEATING COMPONENT TEMPERATURE(8,4)\|TOP OPENING(8,4)\|CHEMICAL ENGINEERING(8,2)\|MATERIALS SCIENCE(8,1)\|ROCK CORROSION SIMULATION EXPERIMENT(8,1)\|HEATING TEMPERATURE(7,4)\|CORROSION CHAMBER BOTTOM OPENING(7,2)\|CARBON DIOXIDE PRESSURE(6,1)\|ROCK CORROSION MAINTENANCE(6,1)\|TEMPERATURE RESISTANT PRESSURE(6,1)\|GAS SOURCE STORAGE TANK(5,9)\|DRIVING CYLINDER(5,5)\|TRANSMISSION PIPE(5,5)\|PRESSURIZED CARBON DIOXIDE(5,4)\|CORROSION CHAMBER TOP OPENING(5,2)\|GEOLOGICAL SEALING ENVIRONMENT(5,1)\|MUTUAL INDEPENDENCE CORROSION CHAMBER(5,1)\|PRESSURE GAUGE(4,10)\|AIR SOURCE STORAGE TANK(4,6)\|LIQUID PHASE ENVIRONMENT(4,4)\|TRANSFER PIPE(4,3)\|CORROSION RESEARCH(4,1)\|POLYTETRAFLUOROETHYLENE COATED WIRE(4,1)\|POLYTETRAFLUOROETHYLENE COVERED WIRE(4,1)\|SEALED LID CORROSION CHAMBER(4,1)\|TEMPERATURE CONTROLLER(3,5)\|DEFECT(3,2)\|	(US20260104346)\|What is claimed is:\|1. An experimental system for assaying rock corrosion in supercritical carbon dioxide, comprising a corrosion vessel (1), wherein:\| the corrosion vessel (1) contains saturated carbon dioxide aqueous solution;\| a top opening of the corrosion vessel (1) is connected with a sealing cover;\| the corrosion vessel (1) is provided with a heating assembly and contains a rock sample placement rack;\| a top of the rock sample placement rack is located above the liquid level of the saturated carbon dioxide aqueous solution, and a bottom of the rock sample placement rack is submerged in the saturated carbon dioxide aqueous solution;\| the heating assembly is arranged on a perimeter wall of the corrosion vessel (1) and connected with a controller (6);\| the controller (6) regulates the temperature of the heating assembly, and is capable of regulating the temperature of the heating assembly to provide conditions for maintaining a carbon dioxide supercritical state;\| the corrosion vessel (1) is connected with a carbon dioxide gas conveying unit through a conveying pipe, and the carbon dioxide gas conveying unit comprises:\| a gas source storage tank (5) configured to supply carbon dioxide gas, wherein the gas source storage tank (5) has a gas outlet;\| a gas booster pump assembly, configured to provide conditions for maintaining a supercritical state of carbon dioxide, wherein the gas booster pump assembly and the gas outlet are connected through a pipeline, and the gas booster pump assembly is connected to the conveying pipe;\| the corrosion vessel (1) comprises two independent corrosion chambers, a first corrosion chamber and a second corrosion chamber, and the first corrosion chamber and the second corrosion chamber are both configured to contain saturated carbon dioxide aqueous solution;\| at least two rock sample placement racks are provided, and each rock sample placement rack is respectively provided in the first corrosion chamber and the second corrosion chamber;\| the sealing cover includes a first sealing cover (2) and a second sealing cover (101);\| the first sealing cover (2) is threadedly connected to the top opening of the first corrosion chamber, and the second sealing cover (101) is threadedly connected to the bottom opening of the second corrosion chamber;\| the delivery pipe includes a first transmission pipe and a second transmission pipe;\| the first transmission pipe and the second transmission pipe are both connected to the gas booster pump assembly through a pipeline;\| the first transmission pipe passes through the first sealing cover (2) and is connected to the first corrosion chamber, and the second transmission pipe is connected to the second corrosion chamber.\|2. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, wherein the gas booster pump assembly comprises a gas booster pump (4) and a buffer vessel (3);\| wherein the buffer vessel (3) is arranged between the gas booster pump (4) and the corrosion vessel (1), and the air inlet of the buffer vessel (3) is connected to the gas booster pump (4) through a pipeline, and the air outlet of the buffer vessel (3) is connected to the corrosion vessel (1) through a conveying pipe.\|3. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 2, wherein the corrosion vessel (1) and the buffer vessel (3) are both made of high-temperature and pressure-resistant anti-corrosion alloy.\|4. The experimental system for rock corrosion in supercritical carbon dioxide according to claim 1, wherein a pressure gauge and a needle pressure control valve configured to regulate carbon dioxide pressure levels are provided on the conveyor pipe.\|5. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, wherein the first sealing cover (2) has a first sealing body (201) threaded with the first corrosion chamber, the second sealing cover (101) has a second sealing body connected with the second corrosion chamber thread, and the first sealing body (201) and the second sealing body are provided with a first sealing ring (202) and a second sealing ring (203) on the upper and lower sleeves.\|6. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, wherein the distance between the first sealing ring (202) and the second sealing ring (203) is 5cm˜5.2cm.\|7. The experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, wherein all pipelines are provided with threaded interfaces at the inlet and outlet ends, and all pipelines are equipped with teflon clad wires on the outside.\|8. A method of using the experimental system for assaying rock corrosion in supercritical carbon dioxide according to claim 1, comprising the following steps:\| a rock sample is placed on the rock sample placement rack, and the saturated carbon dioxide aqueous solution is filled into the corrosion vessel (1), so that the lower part of the rock sample is immersed in the saturated carbon dioxide aqueous solution;\| the gas source storage tank (5) is opened, sending the carbon dioxide in the gas source storage tank (5) into the gas booster pump (4) for pressurization, and the pressurized carbon dioxide is sent into the corrosion vessel (1) through the conveyor pipe;\| the heating temperature of the heating assembly is adjusted by the controller to convert the pressurized carbon dioxide gas fed into the corrosion vessel (1) into supercritical carbon dioxide, so that the rock samples on the rock sample placement rack are placed in the supercritical phase and liquid phase environment.	(US20260104346)\|TECHNICAL FIELD\|[0001] The present invention relates to the field of rock corrosion experimental technology, and more specifically, to an experimental system and method for testing the effects of supercritical carbon dioxide on rock corrosion.\|BACKGROUND\|[0002] Supercritical carbon dioxide rock corrosion assays are used to study the physical and chemical properties of petrochemicals, mainly by testing the changes in chemical composition in rocks to analyze the strength performance of specimens. This type of experiment has a wide range of applications in materials science, chemical engineering, and geological exploration.\|[0003] In a carbon dioxide geological sequestration environment, a rock/supercritical carbon dioxide/carbon dioxide groundwater solution exists in phase equilibrium. Supercritical carbon dioxide can dissolve certain minerals in rock, including carbonate rock, which may lead to changes in the physical and chemical properties of the rock. The carbon-dioxide groundwater solution will react with certain minerals in rock (such as silicates) and may form new mineral phases, which may have different physical and chemical properties, thus affecting the properties of the rock, Thus, it is necessary to study petrology while supercritical carbon dioxide-carbon dioxide groundwater solutions are in coexistence to provide empirical, reliable research data for materials science, chemical engineering and geological exploration. However, there are no device in existence that can provide a suitable environment for exposing rock samples to corrosion in supercritical phase and liquid phase environments at the same temperature and pressure. Accordingly it is of great significance to provide an experimental system to study the corrosion of rock in geological storage environments comprising supercritical carbon dioxide.\|SUMMARY\|[0004] In view of the shortcomings of the above prior art, the purpose of the present invention is to provide an experimental system and usage method for supercritical carbon dioxide rock corrosion, which can corrode rocks in supercritical carbon dioxide and carbon dioxide solution at the same temperature and pressure state of a carbon dioxide geological storage environment.\|[0005] In order to solve the above technical problems, the present invention adopts the following technical scheme:\|[0006] The present invention provides an experimental system for supercritical carbon dioxide rock corrosion, comprising a corrosion vessel, wherein the corrosion vessel is used to store a saturated carbon dioxide aqueous solution. A top opening of the corrosion vessel is connected with a sealing cover, and the inside of the corrosion vessel is provided with a heating assembly and a rock sample placement rack. The top of the rock sample placement rack is located above the liquid level of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is submerged in the saturated carbon dioxide aqueous solution. The heating assembly is arranged on the perimeter wall of the corrosion vessel and is connected with a controller. The controller regulates the temperature of the heating assembly, and is used to make the temperature of the heating assembly suitable for maintaining a supercritical state of carbon dioxide.\|[0007] The corrosion vessel is connected with a carbon dioxide gas conveying unit through a conveying pipe, and the carbon dioxide gas conveying unit comprises:\|[0008] A gas source storage tank, used to supply carbon dioxide gas, wherein the gas source storage tank has a gas outlet;\|[0009] A gas booster pump assembly, used to provide conditions for maintaining a supercritical state of carbon dioxide, wherein the gas booster pump assembly and gas outlet are connected through pipelines, and the gas booster pump assembly is connected to the conveying pipe.\|[0010] Preferably, the gas booster pump assembly comprises a gas booster pump and a buffer vessel, with the buffer vessel arranged between the gas booster pump and the corrosion vessel, and the air inlet of the buffer vessel connected to the gas booster pump through a pipeline. The air outlet of the buffer vessel is connected to the corrosion vessel through a conveying pipe.\|[0011] Preferably, the corrosion vessel and the buffer vessel are made of high-temperature and pressure-resistant anti-corrosion alloy.\|[0012] Preferably, the conveyor pipe is provided with a pressure gauge and a needle pressure control valve for regulating the amount of carbon dioxide pressure.\|[0013] Preferably, the corrosion vessel comprises a first corrosion chamber and a second corrosion chamber. Saturated carbon dioxide aqueous solution is stored in the first corrosion chamber and the second corrosion chamber, and the rock sample placement rack is set in each corrosion chamber. Each rock sample placement rack is arranged in the first corrosion chamber and the second corrosion chamber respectively, and the sealing cover comprises the first sealing cover and the second sealing cover. The first sealing cover is connected with the top open thread of the first corrosion chamber, the second sealing cover is connected with the bottom open thread of the second corrosion chamber via a transmission pipe and a conveyor pipe. The transmission pipe and the conveyor pipe are connected with the gas booster pump assembly through a pipeline, wherein the transmission pipe runs through the first sealing cover and is connected to the first corrosion chamber, and the transfer pipe is connected with the second corrosion chamber.\|[0014] Preferably, the first sealing cover has a first sealing body connected with the first corrosion chamber thread, and the second sealing cover has a second sealing body connected with the second corrosion chamber thread, and the first sealing body and the second sealing body are provided with a first sealing ring and a second sealing ring on the upper and lower sleeves.\|[0015] Preferably, the distance between the first sealing ring and the second sealing ring is 5cm˜5.2cm.\|[0016] Preferably, all pipelines are provided with threaded interfaces at the inlet and outlet ends, and all pipelines are equipped with Teflon clad wires on the outside.\|[0017] The present invention also gives a method for the use of an experimental system for supercritical carbon dioxide rock corrosion, comprising the following steps:\|[0018] The rock sample is placed on the rock sample placement rack, and the corrosion vessel is filled with saturated carbon dioxide aqueous solution, so that the lower part of the rock sample is immersed in the saturated carbon dioxide aqueous solution.\|[0019] Then the gas source storage tank is opened, and the carbon dioxide in the gas source storage tank is sent to the gas booster pump for pressurization. The pressurized carbon dioxide is sent into the corrosion vessel through the conveyor pipe.\|[0020] The heating temperature of the heating component is controlled by the controller to convert the pressurized carbon dioxide gas sent into the corrosion vessel into supercritical carbon dioxide, so that the rock samples on the rock sample placement rack are placed in the supercritical phase and liquid phase environment.\|[0021] The beneficial effects of the present invention compared with the prior art:\|[0022] The experimental system for supercritical carbon dioxide rock corrosion given by the present invention can perform rock corrosion simulation experiments for the carbon dioxide geological storage environment, and solve the disadvantages that the existing devices cannot simulate the carbon dioxide geological storage environment for rock corrosion simulation experiments under the same temperature and pressure state.\|[0023] During experiments, the carbon dioxide gas is pressurized by the gas booster pump assembly and sent into the corrosion vessel through the conveying pipe. In order to make the carbon dioxide feed into the corrosion vessel at a pressure of 7.38 MPa to reach the supercritical state, the temperature of the heating component is controlled by the controller, and the pressurized carbon dioxide sent into the corrosion vessel can reach the temperature of 31.1° C. in the corrosive vessel. Under these conditions when carbon dioxide reaches the supercritical state, the corrosion vessel realizes the simulation of the carbon dioxide geological storage environment. This system overcomes the shortcoming that devices in the existing technology cannot corrode the rock in the liquid phase and the supercritical carbon dioxide gas phase at the same time.\|[0024] The buffer vessel is provided in the present invention not only for sending the high-pressure carbon dioxide gas boosted by the gas booster pump into the buffer vessel for storage, but also for ensuring that the pressurized carbon dioxide gas can be sent into the corrosion vessel at a stable pressure.\|(US20260104346)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0025] FIG. 1 is a schematic diagram of the overall structure of a supercritical carbon dioxide rock corrosion curing test device proposed by the present invention in a high temperature and high pressure environment.\|[0026] FIG. 2 shows the structure of the corrosion vessel.\|[0027] FIG. 3 is a schematic diagram of the structure of the high-pressure sealing cover.\|[0028] FIG. 4 shows the structure of the buffer vessel.\|[0029] FIG. 5 shows the schematic diagram of the gas booster pump structure (front).\|[0030] FIG. 6 shows the schematic diagram of the gas booster pump structure (back).\|[0031] FIG. 7 shows the schematic diagram of the carbon dioxide gas source structure.\|[0032] FIG. 8 shows the structure of the controller, temperature controller, and resistive heating plate.\|(US20260104346)\|REFERENCE NUMERALS\|[0033] 1. Corrosion vessel; 101. a second sealing cover; 102. a first pressure gauge; 103. a first needle pressure regulator; 2. the first sealing cover; 201. The first seal; 202. a first sealing ring; 203. a second sealing ring; 204. a second-needle pressure regulator; 205. a second pressure gauge; 206. The first inlet pipe; 207. High-pressure gas screw interface; 3. Buffer vessel; 301. a pressure buffer tank; 302. the first high-voltage interface screw; 303. a high-pressure gas three-way valve; 304. a second high-voltage interface screw; 305. a second entry pipe; 4. a gas booster pump; 401. a supercharged cylinder block; 402. a drive cylinder; 403. a low air pressure air inlet; 404. a third entry pipe; 405. a high-pressure air outlet; 5. an air source storage tank; 501. a gas pressure reducing valve; 502. an air source switch ball valve; 503. a high-concentration carbon dioxide cylinder; 6. Controller, 601, temperature controller, 602, resistance heating plate.\|DETAILED DESCRIPTION OF EMBODIMENTS\|[0034] The following describes in detail the specific embodiments of the present invention, but it should be understood that the scope of protection of the present invention is not limited by the specific embodiments. Based on the embodiments of the present invention, all other embodiments obtained by persons of ordinary skill in the art without inventive effort are within the scope of protection of the present invention. The experimental methods described in the embodiments of the present invention are conventional methods unless otherwise specified. The inventors have discovered that existing rock corrosion experimental systems all conduct corrosion studies by immersing granite in a high-pressure reactor filled with supercritical carbon dioxide. The experimental device of the present invention primarily considers the coexistence of rock and supercritical CO2—CO2 groundwater solution in a CO2 geological storage environment. Simultaneous corrosion experiments on rock in both environments are more realistic. To address the shortcomings of the prior art, the present invention aims to provide a supercritical CO2 rock corrosion experimental system and method of use. This experimental system can simultaneously corrode rock in both a supercritical state and a CO2 solution in a CO2 geological storage environment. As shown in FIGS. 1 to 8, the present invention provides an experimental system for supercritical carbon dioxide rock corrosion, including a corrosion vessel 1, wherein the corrosion vessel 1 is used to store a saturated carbon dioxide aqueous solution, and the top of the corrosion vessel 1 is open and connected to a sealing cover, and a heating component and a rock sample placement rack are provided inside the corrosion vessel 1, wherein the top of the rock sample placement rack is located above the liquid surface of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is immersed in the saturated carbon dioxide aqueous solution, and the heating component is provided on the peripheral wall of the corrosion vessel 1 and connected to a controller 6, wherein the controller 6 regulates the temperature of the heating component so that the temperature of the heating component after regulation provides a temperature that maintains the supercritical state of carbon dioxide. Conditions are established to ensure that the carbon dioxide delivered into the corrosion vessel 1 reaches a supercritical temperature of 31.1° C. The corrosion vessel 1 is connected to a carbon dioxide gas delivery unit via a delivery pipe. The carbon dioxide gas delivery unit comprises:\|[0035] A gas source tank 5 for supplying carbon dioxide gas and having a gas outlet. The gas source tank 5 comprises a high-concentration carbon dioxide cylinder 503, a gas pressure reducing valve 501, and a gas source on/off ball valve 502. A pipeline is connected to the top of the high-concentration carbon dioxide cylinder 503. The pipeline near the outlet is equipped with a gas source on/off ball valve 502 and a gas pressure reducing valve 501. The gas outlet of the gas source tank 5 is the outlet of the pipeline to which the gas source tank 5 is connected. A gas booster pump assembly is connected to the gas outlet (pipeline output) via a pipeline. The gas booster pump assembly is connected to the delivery pipe. The gas booster pump assembly ensures that the carbon dioxide delivered into the corrosion vessel 1 reaches a supercritical pressure of 7.38 MPa. The gas booster pump assembly includes a gas booster pump 4, which comprises a booster cylinder 401 and a drive cylinder 402. One end of the booster cylinder 401 is connected to the drive cylinder 402. One end of the drive cylinder 402 is provided with a low-pressure air inlet 403, which is connected to the gas source storage tank 5 via a third inlet pipe 404. The drive cylinder 402 is provided with a high-pressure air outlet 405, which is connected to the delivery pipe via a second inlet pipe 305. Specifically, the gas booster pump assembly includes the gas booster pump 4 and a buffer vessel 3. The buffer vessel 3 is located between the gas booster pump 4 and the corrosion vessel 1. The air inlet of the buffer vessel 3 is connected to the gas booster pump 4 via a pipeline, and the air outlet of the buffer vessel 3 is connected to the corrosion vessel 1 via a delivery pipe. Buffer vessel 3 comprises a pressure buffer tank 301, a first high-pressure interface screw 302, a high-pressure gas three-way valve 303, a second high-pressure interface screw 304, and a second inlet pipe 305. The top outlet of the pressure buffer tank 301 is connected to a pipeline via the first high-pressure interface screw 302, which is connected to one outlet of the high-pressure gas three-way valve 303. The second high-pressure interface screw 304 is located at one inlet of the high-pressure gas three-way valve 303 and is threadedly connected to the second inlet pipe 305. The other outlet of the high-pressure gas three-way valve 303 is connected to the corrosion vessel 1 via a delivery pipe. Specifically, both the corrosion vessel 1 and the buffer vessel 3 are made of a high-temperature, pressure-resistant, and corrosion-resistant alloy. This ensures that the materials of the buffer vessel 3 and the corrosion vessel 1 themselves are not corroded by CO2 during long-term corrosion testing, which would otherwise contaminate the specimens with corrosion products. Both the buffer vessel 3 and the corrosion vessel 1 are made of a high-temperature, corrosion-resistant alloy, alloy numbered GH4161. Specifically, the delivery pipe is equipped with a pressure gauge and a needle-type pressure control valve for adjusting the CO2 pressure. The pressure gauge includes a first pressure gauge 102 and a second pressure gauge 205, and the needle pressure control valve includes a first needle pressure regulating valve 103 and a second needle pressure regulating valve 204. This is intended to ensure that the buffer vessel 3 and corrosion vessel 1 materials themselves are not corroded by CO2 during long-term corrosion testing, which would otherwise cause corrosion products from the metal materials to contaminate the specimen. Both the buffer vessel 3 and corrosion vessel 1 are made of a high-temperature corrosion-resistant alloy, alloy number GH4161. Specifically, the corrosion vessel 1 comprises two independent upper and lower first and second corrosion chambers, each containing a saturated carbon dioxide solution. At least two rock sample racks are provided, one in each of the first and second corrosion chambers. The sealing covers comprise a first sealing cover 2 and a second sealing cover 101. The first sealing cover 2 is threadedly connected to the top opening of the first corrosion chamber, while the second sealing cover 101 is threadedly connected to the bottom opening of the second corrosion chamber. The delivery pipe comprises a transmission pipe and a transmission pipe, both of which are connected to the gas booster pump assembly via pipelines. The transmission pipe is connected to the high-pressure gas screw interface 207 at the end of the first inlet pipe 206, passes through the first sealing cover 2, and connects to the first corrosion chamber. The transmission pipe is connected to the second corrosion chamber. The first inlet pipe 206 is also connected to a second needle pressure regulating valve 204 and a second pressure gauge 205, while the transmission pipe is also connected to the first needle pressure regulating valve 103 and a first pressure gauge 102. Specifically, the first sealing cover 2 has a first sealing body 201 threadedly connected to the first corrosion chamber, and the second sealing cover 101 has a second sealing body threadedly connected to the second corrosion chamber. A first sealing ring 202 and a second sealing ring 203 are sleeved above and below the first sealing body 201 and the second sealing body. Specifically, the distance between the first sealing ring 202 and the second sealing ring 203 is 5 cm to 5.2 cm. The first sealing ring 202 is positioned in the middle of the first sealing body 201 or the second sealing body, and the second sealing ring 203 is positioned at the threaded end of the first sealing body 201 or the second sealing body, to provide a tighter connection between the first sealing cover 2 and the first corrosion chamber, or between the second sealing cover 101 and the second corrosion chamber. Specifically, all pipelines have threaded connections at the inlet and outlet ends, and all pipelines are covered with polytetrafluoroethylene (PTFE) wire. The threads at the pipeline connections ensure connection and replacement if damaged. The PTFE wire protects the pipelines from CO2 corrosion and is also wear-resistant. The present invention provides a method for using a supercritical carbon dioxide rock corrosion experimental system, comprising the following steps: Place a rock sample on a rock sample holder, and fill a corrosion vessel 1 with a saturated carbon dioxide aqueous solution so that the lower portion of the rock sample is immersed in the saturated carbon dioxide aqueous solution; Then, open a gas source tank 5, and pump the carbon dioxide in the gas source tank 5 into a gas booster pump 4 for pressurization. The pressurized carbon dioxide is then delivered to the corrosion vessel 1 through a delivery pipe. A controller 6 controls the heating temperature of a heating component to convert the pressurized carbon dioxide gas delivered to the corrosion vessel 1 into supercritical carbon dioxide, thereby placing the rock sample on the rock sample holder in a supercritical and liquid phase environment. Controller 6 includes a temperature controller 601 connected to a resistance heating element 602 for providing a constant temperature heat source for the corrosion vessel 1. The heating element is a resistance heating element 602. The desired temperature is set by the temperature controller 601, and the resistance heating element 602 provides a stable temperature. It is apparent that those skilled in the art may make various modifications and variations to the present invention without departing from the spirit and scope of the present invention. Thus, if these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is intended to include these modifications and variations.	(US20260104346)\|TECHNICAL FIELD\|[0001] The present invention relates to the field of rock corrosion experimental technology, and more specifically, to an experimental system and method for testing the effects of supercritical carbon dioxide on rock corrosion.\|BACKGROUND\|[0002] Supercritical carbon dioxide rock corrosion assays are used to study the physical and chemical properties of petrochemicals, mainly by testing the changes in chemical composition in rocks to analyze the strength performance of specimens. This type of experiment has a wide range of applications in materials science, chemical engineering, and geological exploration.\|[0003] In a carbon dioxide geological sequestration environment, a rock/supercritical carbon dioxide/carbon dioxide groundwater solution exists in phase equilibrium. Supercritical carbon dioxide can dissolve certain minerals in rock, including carbonate rock, which may lead to changes in the physical and chemical properties of the rock. The carbon-dioxide groundwater solution will react with certain minerals in rock (such as silicates) and may form new mineral phases, which may have different physical and chemical properties, thus affecting the properties of the rock, Thus, it is necessary to study petrology while supercritical carbon dioxide-carbon dioxide groundwater solutions are in coexistence to provide empirical, reliable research data for materials science, chemical engineering and geological exploration. However, there are no device in existence that can provide a suitable environment for exposing rock samples to corrosion in supercritical phase and liquid phase environments at the same temperature and pressure. Accordingly it is of great significance to provide an experimental system to study the corrosion of rock in geological storage environments comprising supercritical carbon dioxide.\|SUMMARY\|[0004] In view of the shortcomings of the above prior art, the purpose of the present invention is to provide an experimental system and usage method for supercritical carbon dioxide rock corrosion, which can corrode rocks in supercritical carbon dioxide and carbon dioxide solution at the same temperature and pressure state of a carbon dioxide geological storage environment.\|[0005] In order to solve the above technical problems, the present invention adopts the following technical scheme:\|[0006] The present invention provides an experimental system for supercritical carbon dioxide rock corrosion, comprising a corrosion vessel, wherein the corrosion vessel is used to store a saturated carbon dioxide aqueous solution. A top opening of the corrosion vessel is connected with a sealing cover, and the inside of the corrosion vessel is provided with a heating assembly and a rock sample placement rack. The top of the rock sample placement rack is located above the liquid level of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is submerged in the saturated carbon dioxide aqueous solution. The heating assembly is arranged on the perimeter wall of the corrosion vessel and is connected with a controller. The controller regulates the temperature of the heating assembly, and is used to make the temperature of the heating assembly suitable for maintaining a supercritical state of carbon dioxide.\|[0007] The corrosion vessel is connected with a carbon dioxide gas conveying unit through a conveying pipe, and the carbon dioxide gas conveying unit comprises:\|[0008] A gas source storage tank, used to supply carbon dioxide gas, wherein the gas source storage tank has a gas outlet;\|[0009] A gas booster pump assembly, used to provide conditions for maintaining a supercritical state of carbon dioxide, wherein the gas booster pump assembly and gas outlet are connected through pipelines, and the gas booster pump assembly is connected to the conveying pipe.\|[0010] Preferably, the gas booster pump assembly comprises a gas booster pump and a buffer vessel, with the buffer vessel arranged between the gas booster pump and the corrosion vessel, and the air inlet of the buffer vessel connected to the gas booster pump through a pipeline. The air outlet of the buffer vessel is connected to the corrosion vessel through a conveying pipe.\|[0011] Preferably, the corrosion vessel and the buffer vessel are made of high-temperature and pressure-resistant anti-corrosion alloy.\|[0012] Preferably, the conveyor pipe is provided with a pressure gauge and a needle pressure control valve for regulating the amount of carbon dioxide pressure.\|[0013] Preferably, the corrosion vessel comprises a first corrosion chamber and a second corrosion chamber. Saturated carbon dioxide aqueous solution is stored in the first corrosion chamber and the second corrosion chamber, and the rock sample placement rack is set in each corrosion chamber. Each rock sample placement rack is arranged in the first corrosion chamber and the second corrosion chamber respectively, and the sealing cover comprises the first sealing cover and the second sealing cover. The first sealing cover is connected with the top open thread of the first corrosion chamber, the second sealing cover is connected with the bottom open thread of the second corrosion chamber via a transmission pipe and a conveyor pipe. The transmission pipe and the conveyor pipe are connected with the gas booster pump assembly through a pipeline, wherein the transmission pipe runs through the first sealing cover and is connected to the first corrosion chamber, and the transfer pipe is connected with the second corrosion chamber.\|[0014] Preferably, the first sealing cover has a first sealing body connected with the first corrosion chamber thread, and the second sealing cover has a second sealing body connected with the second corrosion chamber thread, and the first sealing body and the second sealing body are provided with a first sealing ring and a second sealing ring on the upper and lower sleeves.\|[0015] Preferably, the distance between the first sealing ring and the second sealing ring is 5cm˜5.2cm.\|[0016] Preferably, all pipelines are provided with threaded interfaces at the inlet and outlet ends, and all pipelines are equipped with Teflon clad wires on the outside.\|[0017] The present invention also gives a method for the use of an experimental system for supercritical carbon dioxide rock corrosion, comprising the following steps:\|[0018] The rock sample is placed on the rock sample placement rack, and the corrosion vessel is filled with saturated carbon dioxide aqueous solution, so that the lower part of the rock sample is immersed in the saturated carbon dioxide aqueous solution.\|[0019] Then the gas source storage tank is opened, and the carbon dioxide in the gas source storage tank is sent to the gas booster pump for pressurization. The pressurized carbon dioxide is sent into the corrosion vessel through the conveyor pipe.\|[0020] The heating temperature of the heating component is controlled by the controller to convert the pressurized carbon dioxide gas sent into the corrosion vessel into supercritical carbon dioxide, so that the rock samples on the rock sample placement rack are placed in the supercritical phase and liquid phase environment.\|[0021] The beneficial effects of the present invention compared with the prior art:\|[0022] The experimental system for supercritical carbon dioxide rock corrosion given by the present invention can perform rock corrosion simulation experiments for the carbon dioxide geological storage environment, and solve the disadvantages that the existing devices cannot simulate the carbon dioxide geological storage environment for rock corrosion simulation experiments under the same temperature and pressure state.\|[0023] During experiments, the carbon dioxide gas is pressurized by the gas booster pump assembly and sent into the corrosion vessel through the conveying pipe. In order to make the carbon dioxide feed into the corrosion vessel at a pressure of 7.38 MPa to reach the supercritical state, the temperature of the heating component is controlled by the controller, and the pressurized carbon dioxide sent into the corrosion vessel can reach the temperature of 31.1° C. in the corrosive vessel. Under these conditions when carbon dioxide reaches the supercritical state, the corrosion vessel realizes the simulation of the carbon dioxide geological storage environment. This system overcomes the shortcoming that devices in the existing technology cannot corrode the rock in the liquid phase and the supercritical carbon dioxide gas phase at the same time.\|[0024] The buffer vessel is provided in the present invention not only for sending the high-pressure carbon dioxide gas boosted by the gas booster pump into the buffer vessel for storage, but also for ensuring that the pressurized carbon dioxide gas can be sent into the corrosion vessel at a stable pressure.\|(US20260104346)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0025] FIG. 1 is a schematic diagram of the overall structure of a supercritical carbon dioxide rock corrosion curing test device proposed by the present invention in a high temperature and high pressure environment.\|[0026] FIG. 2 shows the structure of the corrosion vessel.\|[0027] FIG. 3 is a schematic diagram of the structure of the high-pressure sealing cover.\|[0028] FIG. 4 shows the structure of the buffer vessel.\|[0029] FIG. 5 shows the schematic diagram of the gas booster pump structure (front).\|[0030] FIG. 6 shows the schematic diagram of the gas booster pump structure (back).\|[0031] FIG. 7 shows the schematic diagram of the carbon dioxide gas source structure.\|[0032] FIG. 8 shows the structure of the controller, temperature controller, and resistive heating plate.\|(US20260104346)\|REFERENCE NUMERALS\|[0033] 1. Corrosion vessel; 101. a second sealing cover; 102. a first pressure gauge; 103. a first needle pressure regulator; 2. the first sealing cover; 201. The first seal; 202. a first sealing ring; 203. a second sealing ring; 204. a second-needle pressure regulator; 205. a second pressure gauge; 206. The first inlet pipe; 207. High-pressure gas screw interface; 3. Buffer vessel; 301. a pressure buffer tank; 302. the first high-voltage interface screw; 303. a high-pressure gas three-way valve; 304. a second high-voltage interface screw; 305. a second entry pipe; 4. a gas booster pump; 401. a supercharged cylinder block; 402. a drive cylinder; 403. a low air pressure air inlet; 404. a third entry pipe; 405. a high-pressure air outlet; 5. an air source storage tank; 501. a gas pressure reducing valve; 502. an air source switch ball valve; 503. a high-concentration carbon dioxide cylinder; 6. Controller, 601, temperature controller, 602, resistance heating plate.\|DETAILED DESCRIPTION OF EMBODIMENTS\|[0034] The following describes in detail the specific embodiments of the present invention, but it should be understood that the scope of protection of the present invention is not limited by the specific embodiments. Based on the embodiments of the present invention, all other embodiments obtained by persons of ordinary skill in the art without inventive effort are within the scope of protection of the present invention. The experimental methods described in the embodiments of the present invention are conventional methods unless otherwise specified. The inventors have discovered that existing rock corrosion experimental systems all conduct corrosion studies by immersing granite in a high-pressure reactor filled with supercritical carbon dioxide. The experimental device of the present invention primarily considers the coexistence of rock and supercritical CO2—CO2 groundwater solution in a CO2 geological storage environment. Simultaneous corrosion experiments on rock in both environments are more realistic. To address the shortcomings of the prior art, the present invention aims to provide a supercritical CO2 rock corrosion experimental system and method of use. This experimental system can simultaneously corrode rock in both a supercritical state and a CO2 solution in a CO2 geological storage environment. As shown in FIGS. 1 to 8, the present invention provides an experimental system for supercritical carbon dioxide rock corrosion, including a corrosion vessel 1, wherein the corrosion vessel 1 is used to store a saturated carbon dioxide aqueous solution, and the top of the corrosion vessel 1 is open and connected to a sealing cover, and a heating component and a rock sample placement rack are provided inside the corrosion vessel 1, wherein the top of the rock sample placement rack is located above the liquid surface of the saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is immersed in the saturated carbon dioxide aqueous solution, and the heating component is provided on the peripheral wall of the corrosion vessel 1 and connected to a controller 6, wherein the controller 6 regulates the temperature of the heating component so that the temperature of the heating component after regulation provides a temperature that maintains the supercritical state of carbon dioxide. Conditions are established to ensure that the carbon dioxide delivered into the corrosion vessel 1 reaches a supercritical temperature of 31.1° C. The corrosion vessel 1 is connected to a carbon dioxide gas delivery unit via a delivery pipe. The carbon dioxide gas delivery unit comprises:\|[0035] A gas source tank 5 for supplying carbon dioxide gas and having a gas outlet. The gas source tank 5 comprises a high-concentration carbon dioxide cylinder 503, a gas pressure reducing valve 501, and a gas source on/off ball valve 502. A pipeline is connected to the top of the high-concentration carbon dioxide cylinder 503. The pipeline near the outlet is equipped with a gas source on/off ball valve 502 and a gas pressure reducing valve 501. The gas outlet of the gas source tank 5 is the outlet of the pipeline to which the gas source tank 5 is connected. A gas booster pump assembly is connected to the gas outlet (pipeline output) via a pipeline. The gas booster pump assembly is connected to the delivery pipe. The gas booster pump assembly ensures that the carbon dioxide delivered into the corrosion vessel 1 reaches a supercritical pressure of 7.38 MPa. The gas booster pump assembly includes a gas booster pump 4, which comprises a booster cylinder 401 and a drive cylinder 402. One end of the booster cylinder 401 is connected to the drive cylinder 402. One end of the drive cylinder 402 is provided with a low-pressure air inlet 403, which is connected to the gas source storage tank 5 via a third inlet pipe 404. The drive cylinder 402 is provided with a high-pressure air outlet 405, which is connected to the delivery pipe via a second inlet pipe 305. Specifically, the gas booster pump assembly includes the gas booster pump 4 and a buffer vessel 3. The buffer vessel 3 is located between the gas booster pump 4 and the corrosion vessel 1. The air inlet of the buffer vessel 3 is connected to the gas booster pump 4 via a pipeline, and the air outlet of the buffer vessel 3 is connected to the corrosion vessel 1 via a delivery pipe. Buffer vessel 3 comprises a pressure buffer tank 301, a first high-pressure interface screw 302, a high-pressure gas three-way valve 303, a second high-pressure interface screw 304, and a second inlet pipe 305. The top outlet of the pressure buffer tank 301 is connected to a pipeline via the first high-pressure interface screw 302, which is connected to one outlet of the high-pressure gas three-way valve 303. The second high-pressure interface screw 304 is located at one inlet of the high-pressure gas three-way valve 303 and is threadedly connected to the second inlet pipe 305. The other outlet of the high-pressure gas three-way valve 303 is connected to the corrosion vessel 1 via a delivery pipe. Specifically, both the corrosion vessel 1 and the buffer vessel 3 are made of a high-temperature, pressure-resistant, and corrosion-resistant alloy. This ensures that the materials of the buffer vessel 3 and the corrosion vessel 1 themselves are not corroded by CO2 during long-term corrosion testing, which would otherwise contaminate the specimens with corrosion products. Both the buffer vessel 3 and the corrosion vessel 1 are made of a high-temperature, corrosion-resistant alloy, alloy numbered GH4161. Specifically, the delivery pipe is equipped with a pressure gauge and a needle-type pressure control valve for adjusting the CO2 pressure. The pressure gauge includes a first pressure gauge 102 and a second pressure gauge 205, and the needle pressure control valve includes a first needle pressure regulating valve 103 and a second needle pressure regulating valve 204. This is intended to ensure that the buffer vessel 3 and corrosion vessel 1 materials themselves are not corroded by CO2 during long-term corrosion testing, which would otherwise cause corrosion products from the metal materials to contaminate the specimen. Both the buffer vessel 3 and corrosion vessel 1 are made of a high-temperature corrosion-resistant alloy, alloy number GH4161. Specifically, the corrosion vessel 1 comprises two independent upper and lower first and second corrosion chambers, each containing a saturated carbon dioxide solution. At least two rock sample racks are provided, one in each of the first and second corrosion chambers. The sealing covers comprise a first sealing cover 2 and a second sealing cover 101. The first sealing cover 2 is threadedly connected to the top opening of the first corrosion chamber, while the second sealing cover 101 is threadedly connected to the bottom opening of the second corrosion chamber. The delivery pipe comprises a transmission pipe and a transmission pipe, both of which are connected to the gas booster pump assembly via pipelines. The transmission pipe is connected to the high-pressure gas screw interface 207 at the end of the first inlet pipe 206, passes through the first sealing cover 2, and connects to the first corrosion chamber. The transmission pipe is connected to the second corrosion chamber. The first inlet pipe 206 is also connected to a second needle pressure regulating valve 204 and a second pressure gauge 205, while the transmission pipe is also connected to the first needle pressure regulating valve 103 and a first pressure gauge 102. Specifically, the first sealing cover 2 has a first sealing body 201 threadedly connected to the first corrosion chamber, and the second sealing cover 101 has a second sealing body threadedly connected to the second corrosion chamber. A first sealing ring 202 and a second sealing ring 203 are sleeved above and below the first sealing body 201 and the second sealing body. Specifically, the distance between the first sealing ring 202 and the second sealing ring 203 is 5 cm to 5.2 cm. The first sealing ring 202 is positioned in the middle of the first sealing body 201 or the second sealing body, and the second sealing ring 203 is positioned at the threaded end of the first sealing body 201 or the second sealing body, to provide a tighter connection between the first sealing cover 2 and the first corrosion chamber, or between the second sealing cover 101 and the second corrosion chamber. Specifically, all pipelines have threaded connections at the inlet and outlet ends, and all pipelines are covered with polytetrafluoroethylene (PTFE) wire. The threads at the pipeline connections ensure connection and replacement if damaged. The PTFE wire protects the pipelines from CO2 corrosion and is also wear-resistant. The present invention provides a method for using a supercritical carbon dioxide rock corrosion experimental system, comprising the following steps: Place a rock sample on a rock sample holder, and fill a corrosion vessel 1 with a saturated carbon dioxide aqueous solution so that the lower portion of the rock sample is immersed in the saturated carbon dioxide aqueous solution; Then, open a gas source tank 5, and pump the carbon dioxide in the gas source tank 5 into a gas booster pump 4 for pressurization. The pressurized carbon dioxide is then delivered to the corrosion vessel 1 through a delivery pipe. A controller 6 controls the heating temperature of a heating component to convert the pressurized carbon dioxide gas delivered to the corrosion vessel 1 into supercritical carbon dioxide, thereby placing the rock sample on the rock sample holder in a supercritical and liquid phase environment. Controller 6 includes a temperature controller 601 connected to a resistance heating element 602 for providing a constant temperature heat source for the corrosion vessel 1. The heating element is a resistance heating element 602. The desired temperature is set by the temperature controller 601, and the resistance heating element 602 provides a stable temperature. It is apparent that those skilled in the art may make various modifications and variations to the present invention without departing from the spirit and scope of the present invention. Thus, if these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is intended to include these modifications and variations.	Family Number\|(115489354)\|115489354\|Advantages / Prev. Drawbacks\|(CN120404566 A)\|In a carbon dioxide geological sequestration environment , rock - supercritical carbon dioxide - carbon dioxide groundwater solutions are in coexistence , supercritical carbon ( . . . ) physical and chemical properties of the rock , while carbon dioxide groundwater solutions can react with certain minerals in the rock ( such as silicate ) , which may generate new mineral phases , which may have different physical and chemical properties , thereby affecting the properties of the rock , so that it is necessary to study the rock properties while supercritical carbon dioxide - carbon ( . . . ) \|(CN120404566B B)\|In a carbon dioxide geological sequestration environment , rock - supercritical carbon dioxide - carbon dioxide groundwater solutions are in coexistence , supercritical carbon ( . . . ) physical and chemical properties of the rock , while carbon dioxide groundwater solutions can react with certain minerals in the rock ( such as silicate ) , which may generate new mineral phases , which may have different physical and chemical properties , thereby affecting the properties of the rock , so that it is necessary to study the rock properties while supercritical carbon dioxide - carbon ( . . . ) \|	Analysis of biological materials\|Measurement	G01N-017/00\|G01N-017/00/2\|G01N-017/00/4\|G01N-017/00/6\|G01N-033/24		G01N-017/00\|G01N-017/00/2\|G01N-017/00/4\|G01N-017/00/6\|G01N-033/24	G01N-017/00\|G01N-033/24	G01N-017/00\|G01N-033/24					CN119959123\|CN119715348\|CN212844929U\|CN206863025U\|CN118226006\|CN112326484	CN119959123 114498188 WHO=Examiner SELF=N CAT=A\|CN119715348 113968326 WHO=Examiner SELF=Y CAT=A\|CN212844929U 93388591 WHO=Examiner SELF=N CAT=A\|CN206863025U 78357085 WHO=Examiner SELF=Y CAT=A\|CN118226006 110304989 WHO=Examiner SELF=N\|CN112326484 92618298 WHO=Examiner SELF=N		\|CN206863025U; CN212844929U; CN119715348; CN119959123; CN118226006; CN112326484		GRANTED	(US20260104346)\|PENDING\|(CN120404566)\|GRANTED	ALIVE	(US20260104346)\|ALIVE\|(CN120404566)\|ALIVE	(US20260104346)\|LEGAL DETAILS FOR US20260104346\|Actual or expected expiration date=2045-12-15\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2025-12-15\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US19420413\|Application date=2025-12-15\|Standardized application number=2025US-19420413\|Event publication date=2026-04-16\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20260104346\|Publication stage code=A1\|Publication date=2026-04-16\|Standardized publication number=US20260104346\|(CN120404566)\|LEGAL DETAILS FOR CN120404566\|Actual or expected expiration date=2045-07-07\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2025-07-07\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN202510926442\|Application date=2025-07-07\|Standardized application number=2025CN-0926442\|Event publication date=2025-08-01\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN120404566\|Publication stage code=A\|Publication date=2025-08-01\|Standardized publication number=CN120404566\|Event publication date=2025-08-01\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2025-08-19\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2025-09-05\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN120404566\|Publication stage code=B\|Publication date=2025-09-05\|Standardized publication number=CN120404566B\|Event publication date=2025-09-05\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right		(US20260104346)\|US\|(CN120404566)\|CN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=lOckPE/DvcMs4KvXHfo1KF90CpEah8ymJjY7t3dG27jB3cyffD7Soc3HTZ4K3xLA34T3rrXcRGc=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023424804&ekey=1966&xpn=US20260104346&kind=A1	https://data.uspto.gov/patent-file-wrapper/search/details/19420413/application-data	https://permalink.orbit.com/RenderStaticFirstPage?XPN=%252F4P%252Bo1Atd%252FXzAir%252FMtFSLMRHIQdPpfyajIQBIFKxQPE%3D%26n%3D1&id=0&base=FAMPAT	CN	(US20260104346)\|CN\|(CN120404566)\|CN\|(CN120404566)\|CN	(US20260104346)\|NAME=Shaoxing University , CITY=Shaoxing City , COUNTRY=CN , ATYP=Non-US Company NAME=China University of Mining and Technology , CITY=Xuzhou , COUNTRY=CN , ATYP=Non-US Company\|(CN120404566)\|NAME=CHINA UNIVERSITY OF MINING & TECHNOLOGY , COUNTRY=CN\|(CN120404566)\|NAME=CHINA UNIVERSITY OF MINING & TECHNOLOGY , COUNTRY=CN		(CN120404566)\|NAME=JI LI;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223\|(CN120404566)\|NAME=JI LI;XI‘AN MINGZE INTELLECTUAL PROPERTY AGENCY (GENERAL PARTNERSHIP) , REG=61223	(US20260104346)\|CN; CN; CN; CN; CN; CN\|(CN120404566)\|CN\|(CN120404566)\|CN	(US20260104346)\|NAME=YANG Shengqi, CITY=Shaoxing City, COUNTRY=CN \|NAME=LI Yue, CITY=Shaoxing City, COUNTRY=CN \|NAME=HUANG Yanhua, CITY=Shaoxing City, COUNTRY=CN \|NAME=YIN Pengfei, CITY=Shaoxing City, COUNTRY=CN \|NAME=TIAN Wenling, CITY=Shaoxing City, COUNTRY=CN \|NAME=ZHU Zhennan, CITY=Shaoxing City, COUNTRY=CN\|(CN120404566)\|NAME=YANG SHENGQI, COUNTRY=CN \|NAME=LI YUE\|NAME=HUANG YANHUA\|NAME=YIN PENGFEI\|NAME=TIAN WENLING\|NAME=ZHU ZHENNAN\|(CN120404566)\|NAME=YANG SHENGQI, COUNTRY=CN \|NAME=LI YUE\|NAME=HUANG YANHUA\|NAME=YIN PENGFEI\|NAME=TIAN WENLING\|NAME=ZHU ZHENNAN	(US20260104346)\|8\|(CN120404566)\|8	1	2					(US20260104346)\|Number of Claims: NCL=8\|Number of Drawings: NDR=8\|Number of Figures: NFG=8\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|\|(CN120404566)\|Number of Claims: NCL=8\|Gazette date: GAZDATE=2025-09-05\|Gazette number: GAZNUM=41-3602\|Substantial examination effective date: 20250819 Examination duration: 0 months\|Number of Pages: NPAGES=15\|Primary examiner: 韩莉莉\|Primary examiner: Han Lili\|\|(CN120404566)\|Number of Claims: NCL=9\|Gazette date: GAZDATE=2025-08-01\|Gazette number: GAZNUM=41-3102\|Number of Pages: NPAGES=15\|Primary examiner: 韩莉莉\|Primary examiner: Han Lili\|	(CN120404566)\|Previous publication: CN120404566 A 2025-08-01 [CN120404566]	(US20260104346)\|ENGLISH (ENG)	(US20260104346)\|Patent\|(CN120404566B)\|Patent\|(CN120404566)\|Patent	Titre: (US20260104346)\|An Experimental System for Rock Corrosion by Supercritical Carbon Dioxide Résumé: (US20260104346)\|The present invention relates to an experimental system and usage method for supercritical carbon dioxide rock corrosion. The experimental system comprises a corrosion vessel for exposing samples to a saturated carbon dioxide aqueous solution. The inside of the corrosion vessel is provided with a heating assembly and a rock sample placement rack. The top of the rock sample placement rack is above the liquid level of saturated carbon dioxide aqueous solution, and the bottom of the rock sample placement rack is submerged in saturated carbon dioxide aqueous solution. The heating assembly is located on the perimeter wall of the corrosion vessel and connected with a controller. The corrosion vessel is connected to a carbon dioxide gas delivery unit and a booster pump assembly connected via a conveying pipe. The present invention enables rocks to corrode in both supercritical and carbon dioxide solutions.	40	Abstract	gpt-4o-mini	no	The focus is on an experimental system for rock corrosion using supercritical CO₂, not on accelerating mineral weathering for CO₂ capture.
42	US61/152,146P\|US61/152,146\|US12/703,560\|WOUS2010/023874	VE2010-000232\|WOUS2010/023874\|MA34158\|IN1891/MUMNP/2011\|ZA201106555\|EG2011081356\|TN2011000392\|IL214550\|BRPI1008552\|CN201080016465\|EP10741714\|MX2011008534\|UAA201110794\|AU2010213774\|EA201171025\|AP201105875\|CA2752133\|MYPI2011003744\|PE2011001479\|US12/703,560	VE2010000232\|BRPI1008552\|CN102395653\|MY152426\|EP2406351\|MX320012\|UA104617\|EG26419\|AU2010213774\|TN2011000392\|US8349171\|BRPI1008552\|VE2010000232\|PE20120707\|ZA201106555\|CN102395653\|MA33113\|EA201171025\|IN1891/MUMNP/2011\|EP2406351\|MX2011008534\|AP2011005875\|AP201105875\|IL214550\|AU2010213774\|WO2010/093777\|CA2752133\|WO2010/093777\|US20100200467	35292	VE2010000232 B 2021-12-13 [VE2010000232]\|VE2010000232 A 2012-07-26 [VE2010000232]\|WO2010/093777 A3 2010-12-09 [WO201093777]\|WO2010/093777 A2 2010-08-19 [WO201093777]\|MA33113 B1 2012-03-01 [MA--33113]\|IN1891/MUMNP/2011 A 2012-02-03 [IN2011MN01891]\|ZA201106555 B 2012-05-30 [ZA201106555]\|EG26419 A 2013-10-23 [EG--26419]\|TN2011000392 A1 2013-03-27 [TN2011000392]\|IL214550 A 2011-09-27 [IL-214550]\|BRPI1008552 A2 2016-03-15 [BR201008552]\|BRPI1008552 A0 2012-11-20 [BR201008552]\|CN102395653 B 2015-05-06 [CN102395653B]\|CN102395653 A 2012-03-28 [CN102395653]\|EP2406351 A4 2014-09-17 [EP2406351]\|EP2406351 A2 2012-01-18 [EP2406351]\|MX320012 B 2014-05-05 [MX-320012]\|MX2011008534 A 2011-12-16 [MX2011008534]\|UA104617 C2 2014-02-25 [UA-104617]\|AU2010213774 B2 2013-06-13 [AU2010213774]\|AU2010213774 A1 2011-09-22 [AU2010213774]\|EA201171025 A1 2012-02-28 [EA201171025]\|AP201105875 D0 2011-10-31 [AP201105875]\|AP2011005875 A0 2011-10-31 [AP2011005875]\|CA2752133 A1 2010-08-19 [CA2752133]\|MY152426 A 2014-09-30 [MY-152426]\|PE20120707 A1 2012-06-27 [PE201200707]\|US8349171 B2 2013-01-08 [US8349171]\|US20100200467 A1 2010-08-12 [US20100200467]	2009-02-12\|2010-02-10\|2010-02-11	2010-02-12\|2010-02-11\|2011-09-09\|2011-09-09\|2011-09-07\|2011-08-11\|2011-08-09\|2011-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-11\|2010-02-10	2021-12-13\|2016-03-15\|2015-05-06\|2014-09-30\|2014-09-17\|2014-05-05\|2014-02-25\|2013-10-23\|2013-06-13\|2013-03-27\|2013-01-08\|2012-11-20\|2012-07-26\|2012-06-27\|2012-05-30\|2012-03-28\|2012-03-01\|2012-02-28\|2012-02-03\|2012-01-18\|2011-12-16\|2011-10-31\|2011-10-31\|2011-09-27\|2011-09-22\|2010-12-09\|2010-08-19\|2010-08-19\|2010-08-12	\|(US8349171)\|2013-01-08\|\|(CN102395653B)\|2015-05-06\|(VE2010000232)\|2021-12-13\|(MY-152426)\|2014-09-30\|(MX-320012)\|2014-05-05\|(UA-104617)\|2014-02-25\|(EG--26419)\|2013-10-23\|(AU2010213774)\|2013-06-13\|(ZA201106555)\|2012-05-30\|(MA--33113)\|2012-03-01\|\|\|\|\|\|\|\|	(EP2406351)\|2015-03-20\|(US8349171)\|2025-02-10\|(WO2010/093777)\|2012-08-12\|(CN102395653)\|2016-02-11\|(VE2010000232)\|2030-02-12\|(MY152426)\|2030-02-11\|(MX320012)\|2030-02-11\|(UA104617)\|2030-02-11\|(EG26419)\|2030-02-11\|(AU2010213774)\|2016-09-08\|(ZA201106555)\|2030-02-11\|(MA33113)\|2030-02-11\|(BRPI1008552)\|2016-09-13\|(TN2011000392)\|2030-02-11\|(PE20120707)\|2016-01-29\|(EA201171025)\|2017-02-28\|(IN1891/MUMNP/2011)\|2022-02-03\|(AP201105875)\|2016-10-31\|(IL214550)\|2016-09-27\|(CA2752133)\|2016-02-11	(EP2406351)\|Methods of recovering hydrocarbons from hydrocarbonaceous material using a constructed infrastructure and associated systems maintained under positive pressure	(EP2406351)\|A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure (100). This constructed infrastructure (100) defines a substantially encapsulated volume. A comminuted hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body (120) of hydrocarbonaceous material. The permeable body (120) can be heated sufficient to remove hydrocarbons therefrom. During heating and removal of hydrocarbons and subsequent thereto a positive pressure can be maintained within the encapsulated volume by means of a non-oxidizing gas to expedite flushing of hydrocarbonaceous material, inhibit unwanted entry of oxygen into the encapsulated volume and remove recoverable hydrocarbons following the heating process.	RED LEAF RESOURCES	(EP2406351)\|Red Leaf Resources, Inc. ([US])\|(EP2406351)\|Red Leaf Resources, Inc. ([US])\|(US8349171)\|Red Leaf Resources, Inc. ([US])\|(US20100200467)\|DANA TODD\|PATTEN JAMES W\|(WO2010/093777)\|RED LEAF RESOURCES, INC.\|(WO2010/093777)\|RED LEAF RESOURCES, INC. ([US])\|(CN102395653)\|RED LEAF RESOURCES INC. ([US])\|(CN102395653)\|RED LEAF RESOURCES INC. ([US])\|\|\|(MY152426)\|RED LEAF RESOURCES, INC.\|(MX320012)\|RED LEAF RESOURCES INC* ([US])\|(MX2011008534)\|RED LEAF RESOURCES INC*\|(UA104617)\|RED LEAF RESOURCES, INC.\|(EG26419)\|RED LEAF RESOURCES INC\|(AU2010213774)\|Red Leaf Resources, Inc.\|(AU2010213774)\|Red Leaf Resources, Inc.\|(ZA201106555)\|RED LEAF RESOURCES INC\|(MA33113)\|RED LEAF RESOURCES, INC.\|(BRPI1008552)\|RED LEAF RESOURCES, INC.\|\|(TN2011000392)\|RED LEAF RESOURCES, INC.\|(PE20120707)\|RED LEAF RESOURCES, INC.\|\|(IN1891/MUMNP/2011)\|RED LEAF RESOURCES INC ([US])\|\|(AP2011005875)\|RED LEAF RESOURCES INC\|(IL214550)\|RED LEAF RESOURCES, INC\|(CA2752133)\|RED LEAF RESOURCES, INC. ([US])	DANA TODD\|PATTEN JAMES W	(EP2406351)\|DANA, Todd\|PATTEN, James, W.\|(EP2406351)\|DANA, Todd\|PATTEN, James, W.	(EP2406351)\|Walker, Ross Thomson;Forresters ([DE])\|Reg. Nb: 101298687\|(US8349171)\|Thorpe North & Western LLP\|(WO2010/093777)\|Ericksen Erik S. et al. ([US])\|(CN102395653)\|ZHAO RONGMIN;JEEKAI & PARTNERS\|Reg. Nb: 11245\|(VE2010000232)\|LINARES ALLOCA MARLIN ENEIDA\|(MX320012)\|MARIA ANGELICA PARDAVELL JUAREZ\|(AU2010213774)\|FB Rice ([AU])\|(CA2752133)\|BERESKIN & PARR LLP/S.E.N.C.R.L.,S.R.L. ([CA])	(US8349171)\|As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required.\|Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|In some cases it can be desirable to provide a single type of hydrocarbonaceous material so that the permeable body consists essentially of one of the above materials.\|In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants. This approach uniquely provides solutions to problems for not just one, but many problems, and in an integrated approach.\|More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body.\|Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like.\|	(US8349171)\|1. A method of recovering hydrocarbons from hydrocarbonaceous materials, comprising: a) forming a constructed permeability control infrastructure which defines a substantially encapsulated volume; b) introducing a comminuted hydrocarbonaceous material into the control infrastructure to form a permeable body of hydrocarbonaceous material; c) maintaining within said encapsulated volume a positive pressure relative to the pressure outside of said control infrastructure; d) heating the hydrocarbonaceous material sufficient to remove hydrocarbons therefrom such that the hydrocarbonaceous material is substantially stationary during heating; e) flushing a gaseous fluid substantially free of oxygen throughout the permeable body in order to substantially remove hydrocarbons and other gaseous components from the permeable body, wherein heating of said hydrocarbonaceous materials has been terminated and said gaseous fluid is passed throughout the permeable body at a low temperature relative to the temperature at which said hydrocarbonaceous materials have been heated to provide a cooling effect on said hydrocarbonaceous materials and flush residual hydrocarbons and other gaseous materials from within said encapsulated volume; and f) collecting removed hydrocarbons and other gaseous components.\|16. A constructed permeability control infrastructure, comprising: a) a permeability control impoundment defining a substantially encapsulated volume, said impoundment having a foundation structural floor support of earthen material or local surface topography as a floor; and b) a comminuted hydrocarbonaceous material within the encapsulated volume forming a substantially stationary permeable body of hydrocarbonaceous material, wherein the impoundment is adapted such that a positive pressure is maintained in said encapsulated volume relative to the pressure outside of said control infrastructure and prevents the introduction of air or other oxidizing gases from entering the impoundment.\|	(US8349171)\|In another aspect, walls of the impoundment can be acid, water and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water.\|In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|In yet another detailed aspect, the permeable body can further comprise an additive or biomass.\|	(US8349171)\|HYDROCARBONACEOUS MATERIAL(100,43)\|INFRASTRUCTURE(100,25)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|CONSTRUCTED PERMEABILITY(100,16)\|POSITIVE PRESSURE(100,15)\|RECOVERING HYDROCARBON(100,12)\|ENCAPSULATED VOLUME(91,25)\|FOUNDATION FLOOR STRUCTURE(76,2)\|FLUSH RESIDUAL HYDROCARBON(69,1)\|BENTONITE CLAY(67,5)\|GASEOUS FLUID(63,4)\|ATMOSPHERIC POLLUTANT(58,1)\|GASEOUS COMPONENT(54,2)\|GEOTEXTILE BAG(53,3)\|IMPOUNDMENT(52,65)\|SOLVENT RECOVERY(52,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(51,6)\|CLAY LINING(49,1)\|ACID HALIDE(47,1)\|RESIN ION EXCHANGE(47,1)\|METHANEDIONE PRODUCTION(46,1)\|SYNTHETIC GEOGRID(45,3)\|OIL SHALE ORE(42,1)\|CARBONATE DECOMPOSITION(41,2)\|SYNTHETIC CLAY(40,1)\|ENORMOUS VOLUME CAPACITY(39,1)\|COLLECTING REMOVED HYDROCARBON(37,1)\|CO2 EMISSION(36,2)\|CONTROL INFRASTRUCTURE(35,22)\|OXIDIZING GAS(35,2)\|TEMPERATURE GEOMEMBRANE(35,1)\|SOLUTION MINING(33,1)\|REFRACTORY CEMENT(32,6)\|POLYMERIC RESIN(32,3)\|PERMEABILITY(31,24)\|BRINE SOLUTION(31,1)\|ELECTROPLATING(31,1)\|EXTRACT FLUID(31,1)\|REBAR(29,5)\|FLOTATION(29,1)\|IMPOUNDMENT WALL(28,12)\|LEACHING(28,1)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|GASEOUS MATERIAL(27,3)\|GUIDELINE(26,4)\|PERMEABILITY CONTROL IMPOUNDMENT(26,4)\|HYDROCARBON COMBUSTION(26,3)\|HYDROCARBONACEOUS MATERIAL FLUSHING(26,1)\|FIBERGLASS(23,5)\|BRINE(23,1)\|PRECIPITATION(22,2)\|EARTHEN MATERIAL(21,4)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|VOID SPACE(20,5)\|SEALANT(20,2)\|MALFUNCTION(20,1)\|BIOMASS(19,3)\|SECTIONED CAPSULE IMPOUNDMENT(19,2)\|ADDITIVE(18,13)\|STOICHIOMETRIC CONDITION(18,3)\|TOTAL VOLUME(18,2)\|COMPACTED FILL CEILING(17,3)\|GROUT(17,3)\|DRAIN PIPE(17,1)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(17,1)\|MECHANICAL INTEGRITY(17,1)\|HYDRO CARBONACEOUS DEPOSIT EXCAVATION(16,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(16,1)\|RESISTANCE HEATER(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|INFRASTRUCTURE OPERATING TEMPERATURE(15,1)\|QUARRY CAPSULE IMPOUNDMENT(15,1)\|UNCAPPED CAPSULE IMPOUNDMENT(15,1)\|UNDERGROUND RUBBLE CHIMNEY(15,1)\|EXTRACTION(14,2)\|NANOCARBON FULLERENE ADDITIVE(14,1)\|STRUCTURED IMPOUNDMENT CAPSULE(14,1)\|HYDROCARBON PRODUCTION(13,12)\|PROPANE(12,6)\|CONTAINMENT CAPSULE(12,2)\|NEARBY IMPOUNDMENT(12,2)\|TAILING BERM(12,2)\|UNRECOVERED HYDROCARBON(12,2)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|COAL(11,7)\|PEAT(11,4)\|ECONOMIC VALUE(11,1)\|ENGINEERED PERMEABILITY BARRIER(11,1)\|HYDROCARBON LEAN SHALE(11,1)\|HYDROCARBON UNCONTROLLED EGRESS(11,1)\|UNDERGROUND MINED HYDROCARBON(11,1)\|VOID VOLUME(10,7)\|FUEL CELL(10,5)\|RADIO FREQUENCY(10,4)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|BENCH MINING ELEVATION(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|ECONOMICALLY COMPETITIVE RECOVERY(10,1)\|EXTERIOR CAPSULE IMPOUNDMENT(10,1)\|GARBAGE IMPOUNDMENT(10,1)\|GRAVITY ASSISTED DRAINAGE PIPE(10,1)\|GRAVITY DRAINAGE ASSISTANCE(10,1)\|INDISCRIMINATE DUMPING(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|MANIPULATED GRADE SHALE(10,1)\|MEDIAN SIZE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|UNTAPPED RESOURCE(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|HEAT PIPE(9,6)\|CONSTRUCTED SULFUR CAPSULE(9,2)\|IMPOUNDMENT HEIGHT(9,2)\|PRECIOUS METAL(8,5)\|IMPERMEABLE FLOOR LAYER(8,3)\|SURFACE TOPOGRAPHY(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CORE DRILLING(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|HYDROCARBONACEOUS DEPOSIT(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MINING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|LIQUID PRODUCT(7,11)\|HYDRO CARBONACEOUS MATERIAL(7,4)\|CONVECTIVE HEATING(7,2)\|CRUSHED GLASS(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HEATED CONDUIT(7,2)\|HEATING(7,2)\|HORIZONTAL MINING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|BIO LEACHING(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HEATING RESIDENCE TIME(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PERMEABILITY BALANCE(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|HEAT TRANSFER(6,10)\|HYDROGEN DONOR(6,7)\|HEAVY METAL(6,5)\|BLASTING(6,3)\|CONVECTION(6,3)\|FREEZE WALL(6,3)\|ECONOMICS(6,2)\|FLOOR CONSTRUCTION(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENCLOSED CAPSULE(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MAXIMIZE RECOVERY(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|KEROGEN OIL(5,4)\|HEATED FLUID(5,3)\|PIPING(5,3)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|ANAEROBIC CONDITION(5,1)\|AQUEOUS SLURRY(5,1)\|BARRIER MANUFACTURE(5,1)\|CAPACITY INDICATOR(5,1)\|CAPSULE IMPOUNDMENT AREA(5,1)\|CATALYZING GAS(5,1)\|CEILING CAP(5,1)\|CLAY PIPE(5,1)\|CO2 PRODUCTION(5,1)\|COMMINUTED MASS(5,1)\|COMPOSITION ADMIXTURE(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|DECREASED VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLUID DRAINAGE(5,1)\|FLUSHING GAS(5,1)\|FUTURE DATE(5,1)\|GAS COMBUSTION HEATER(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GASEOUS LIGHT HYDROCARBON(5,1)\|GEO MEMBRANE LAYER(5,1)\|GEO SYNTHETIC MEMBRANE(5,1)\|GEOLOGICAL LOCATION(5,1)\|HEATING CONDUIT PLACEMENT(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|IMPOUNDMENT USEFUL LIFE(5,1)\|INORGANIC MATTER(5,1)\|KEROGEN REMOVAL(5,1)\|LAYER COMPACTION(5,1)\|LONG HEATING RESIDENCE TIME(5,1)\|MICROBIOLOGY(5,1)\|MINIMAL WASTE(5,1)\|MINING HAUL TRUCK NEED(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONOXIDIZING GAS(5,1)\|OIL BLEND(5,1)\|OPTIMIZATION REASON(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|PRECAST PIECE(5,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(5,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(5,1)\|QUALITY DETERIORATION(5,1)\|RECOVERED HYDROCARBON LIQUID(5,1)\|RECOVERING OIL(5,1)\|REFORMATION(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RESIDUAL SHALE REDUCED WETTING(5,1)\|RICH OIL BEARING ORE(5,1)\|ROTATING RETORT(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT CLOSER(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|STAGED PROCESSING(5,1)\|STEAM INJECTION(5,1)\|TECHNICAL CHALLENGE(5,1)\|TREMENDOUS VOLUME(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNCONTROLLED MIGRATION PREVENTION(5,1)\|VAPOROUS COMPONENT(5,1)\|VARIED ENZYME(5,1)\|VOLATILE ORGANIC(5,1)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOMATERIAL(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DIFFICULT CHALLENGE(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|FUNCTION VOID SPACE(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|\|(US20100200467)\|HYDROCARBONACEOUS MATERIAL(100,42)\|INFRASTRUCTURE(100,22)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,15)\|CONSTRUCTED PERMEABILITY(100,12)\|RECOVERING HYDROCARBON(100,12)\|ENCAPSULATED VOLUME(87,25)\|GASEOUS FLUID(60,5)\|ATMOSPHERIC POLLUTANT(58,1)\|GASEOUS COMPONENT(54,2)\|SOLVENT RECOVERY(52,2)\|COMMINUTED HYDRO CARBONACEOUS MATERIAL(51,1)\|CLAY LINING(49,1)\|ACID HALIDE(47,1)\|RESIN ION EXCHANGE(47,1)\|METHANEDIONE PRODUCTION(46,1)\|OIL SHALE ORE(42,1)\|BENTONITE CLAY(41,3)\|CARBONATE DECOMPOSITION(41,2)\|SYNTHETIC CLAY(40,1)\|ENORMOUS VOLUME CAPACITY(39,1)\|FLUSH RESIDUAL HYDROCARBON(39,1)\|FLUSH HYDROCARBON VAPOR(38,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(37,5)\|COLLECTING REMOVED HYDROCARBON(37,1)\|CO2 EMISSION(36,2)\|CONTROL INFRASTRUCTURE(35,22)\|TEMPERATURE GEOMEMBRANE(35,1)\|SOLUTION MINING(33,1)\|PERMEABILITY(31,24)\|BRINE SOLUTION(31,1)\|ELECTROPLATING(31,1)\|EXTRACT FLUID(31,1)\|FLOTATION(29,1)\|IMPOUNDMENT WALL(28,12)\|LEACHING(28,1)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|GUIDELINE(26,4)\|PERMEABILITY CONTROL IMPOUNDMENT(26,4)\|HYDROCARBON COMBUSTION(26,3)\|HYDROCARBONACEOUS MATERIAL FLUSHING(26,1)\|HYDRO CARBONACEOUS MATERIAL(23,5)\|BRINE(23,1)\|GASEOUS MATERIAL(22,3)\|PRECIPITATION(22,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|VOID SPACE(20,5)\|SEALANT(20,2)\|MALFUNCTION(20,1)\|REFRACTORY CEMENT(19,4)\|BIOMASS(19,3)\|SECTIONED CAPSULE IMPOUNDMENT(19,2)\|ADDITIVE(18,13)\|STOICHIOMETRIC CONDITION(18,3)\|TOTAL VOLUME(18,2)\|COMPACTED FILL CEILING(17,3)\|GROUT(17,3)\|REBAR(17,3)\|DRAIN PIPE(17,1)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(17,1)\|MECHANICAL INTEGRITY(17,1)\|HYDRO CARBONACEOUS DEPOSIT EXCAVATION(16,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(16,1)\|RESISTANCE HEATER(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|HEATED HYDROCARBONACEOUS MATERIAL(15,1)\|INFRASTRUCTURE OPERATING TEMPERATURE(15,1)\|QUARRY CAPSULE IMPOUNDMENT(15,1)\|UNCAPPED CAPSULE IMPOUNDMENT(15,1)\|UNDERGROUND RUBBLE CHIMNEY(15,1)\|EXTRACTION(14,2)\|NANOCARBON FULLERENE ADDITIVE(14,1)\|STRUCTURED IMPOUNDMENT CAPSULE(14,1)\|HYDROCARBON PRODUCTION(13,12)\|PROPANE(12,6)\|CONTAINMENT CAPSULE(12,2)\|NEARBY IMPOUNDMENT(12,2)\|TAILING BERM(12,2)\|UNRECOVERED HYDROCARBON(12,2)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|COAL(11,7)\|PEAT(11,4)\|ECONOMIC VALUE(11,1)\|ENGINEERED PERMEABILITY BARRIER(11,1)\|HYDROCARBON LEAN SHALE(11,1)\|HYDROCARBON UNCONTROLLED EGRESS(11,1)\|UNDERGROUND MINED HYDROCARBON(11,1)\|VOID VOLUME(10,7)\|FUEL CELL(10,5)\|RADIO FREQUENCY(10,4)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|BENCH MINING ELEVATION(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|ECONOMICALLY COMPETITIVE RECOVERY(10,1)\|EXTERIOR CAPSULE IMPOUNDMENT(10,1)\|GARBAGE IMPOUNDMENT(10,1)\|GRAVITY ASSISTED DRAINAGE PIPE(10,1)\|GRAVITY DRAINAGE ASSISTANCE(10,1)\|INDISCRIMINATE DUMPING(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|MANIPULATED GRADE SHALE(10,1)\|MEDIAN SIZE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|UNTAPPED RESOURCE(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|HEAT PIPE(9,6)\|CONSTRUCTED SULFUR CAPSULE(9,2)\|IMPOUNDMENT HEIGHT(9,2)\|PRECIOUS METAL(8,5)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CORE DRILLING(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|HYDROCARBONACEOUS DEPOSIT(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MINING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|LIQUID PRODUCT(7,11)\|CONVECTIVE HEATING(7,2)\|CRUSHED GLASS(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HEATED CONDUIT(7,2)\|HEATING(7,2)\|HORIZONTAL MINING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|BIO LEACHING(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HEATING RESIDENCE TIME(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PERMEABILITY BALANCE(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|HEAT TRANSFER(6,10)\|HYDROGEN DONOR(6,7)\|HEAVY METAL(6,5)\|BLASTING(6,3)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|ECONOMICS(6,2)\|FLOOR CONSTRUCTION(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENCLOSED CAPSULE(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MAXIMIZE RECOVERY(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|KEROGEN OIL(5,4)\|HEATED FLUID(5,3)\|PIPING(5,3)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|ANAEROBIC CONDITION(5,1)\|AQUEOUS SLURRY(5,1)\|BARRIER MANUFACTURE(5,1)\|CAPACITY INDICATOR(5,1)\|CAPSULE IMPOUNDMENT AREA(5,1)\|CATALYZING GAS(5,1)\|CEILING CAP(5,1)\|CLAY PIPE(5,1)\|CO2 PRODUCTION(5,1)\|COMMINUTED MASS(5,1)\|COMPOSITION ADMIXTURE(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|DECREASED VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLUID DRAINAGE(5,1)\|FLUSHING GAS(5,1)\|FUTURE DATE(5,1)\|GAS COMBUSTION HEATER(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GASEOUS LIGHT HYDROCARBON(5,1)\|GEO MEMBRANE LAYER(5,1)\|GEO SYNTHETIC MEMBRANE(5,1)\|GEOLOGICAL LOCATION(5,1)\|HEATING CONDUIT PLACEMENT(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|IMPOUNDMENT USEFUL LIFE(5,1)\|INORGANIC MATTER(5,1)\|KEROGEN REMOVAL(5,1)\|LAYER COMPACTION(5,1)\|LONG HEATING RESIDENCE TIME(5,1)\|MICROBIOLOGY(5,1)\|MINIMAL WASTE(5,1)\|MINING HAUL TRUCK NEED(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONOXIDIZING GAS(5,1)\|OIL BLEND(5,1)\|OPTIMIZATION REASON(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PRECAST PIECE(5,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(5,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(5,1)\|QUALITY DETERIORATION(5,1)\|RECOVERED HYDROCARBON LIQUID(5,1)\|RECOVERING OIL(5,1)\|REFORMATION(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RESIDUAL SHALE REDUCED WETTING(5,1)\|RICH OIL BEARING ORE(5,1)\|ROTATING RETORT(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|STAGED PROCESSING(5,1)\|STEAM INJECTION(5,1)\|TECHNICAL CHALLENGE(5,1)\|TREMENDOUS VOLUME(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNCONTROLLED MIGRATION PREVENTION(5,1)\|VAPOROUS COMPONENT(5,1)\|VARIED ENZYME(5,1)\|VOLATILE ORGANIC(5,1)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOMATERIAL(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DIFFICULT CHALLENGE(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|FUNCTION VOID SPACE(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|\|(CN102395653)\|HYDROCARBONACEOUS MATERIAL(100,46)\|INFRASTRUCTURE CONSTRUCTION(100,23)\|INFRASTRUCTURE(100,22)\|ENCAPSULATED VOLUME(100,21)\|POSITIVE PRESSURE(100,16)\|CONSTRUCTED PERMEABILITY(100,13)\|RECOVERING HYDROCARBON(100,11)\|ECONOMICALLY COMPETITIVE RECOVERY(74,1)\|UNDERGROUND AQUIFER CONTAMINATION(67,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(63,2)\|DIRTY FINE PARTICULATE(63,1)\|COMPACTED FILL(57,6)\|BENTONITE CLAY(56,1)\|GASEOUS COMPONENT(54,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(52,6)\|IMPOUNDMENT(50,64)\|CLAY LINING(50,1)\|GASEOUS FLUID(49,4)\|CONTROL INFRASTRUCTURE(46,23)\|OXIDIZING GAS(45,1)\|SYNTHETIC CLAY(41,1)\|FLUSH HYDROCARBON VAPOR(38,1)\|DRAINAGE PIPE(37,2)\|ECONOMICS(36,1)\|TEMPERATURE GEOMEMBRANE(36,1)\|GAS OXIDATION(34,2)\|DIFFICULT CHALLENGE(34,1)\|BRINE SOLUTION(32,1)\|CLAY(31,7)\|FLUSHING(31,4)\|SOLVENT RECOVERY(30,2)\|HYDROCARBON RESIDUE(30,1)\|PERMEABILITY CONTROL IMPOUNDMENT(29,3)\|OBSERVABLE(29,1)\|IMPOUNDMENT WALL(28,11)\|REMEDIATION(28,2)\|ASSURANCE(28,1)\|ENVIRONMENTAL HAZARD(28,1)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|SEALANT(28,1)\|PERMEABILITY(27,27)\|HYDROCARBON PRODUCTION(25,13)\|ENCLOSED VOLUME(25,7)\|UNDERGROUND MINING(25,2)\|SEGMENTED CAPSULE IMPOUNDMENT(24,3)\|BRINE(23,1)\|FREEZE WALL(22,3)\|GASEOUS MATERIAL(22,3)\|BLASTING(22,2)\|VOID SPACE(21,6)\|AIR PREVENTING(21,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|LEAK(21,1)\|REFRACTORY CEMENT(20,4)\|BIOMASS(20,3)\|REMOVING HYDROCARBON(20,3)\|HYDROCARBON MATERIAL FLUSHING(20,1)\|OUTPUT CAPACITY(20,1)\|REMOVING PRODUCT(20,1)\|ADDITIVE(18,14)\|STOICHIOMETRIC CONDITION(18,3)\|TOTAL VOLUME(18,2)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(18,1)\|PREVENTABLE WATER BODY(18,1)\|GRAVEL(17,3)\|GROUT(17,3)\|REBAR(17,3)\|ADAPTABLE WATER BODY(16,1)\|SURFACE DISTURBANCE(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|BIOCHEMICALLY OXIDIZE ORE(15,1)\|HEATED HYDROCARBONACEOUS MATERIAL(15,1)\|MINE CAPSULE IMPOUNDMENT(15,1)\|WATER POLLUTION(15,1)\|AFT BERM PERMEABILITY(14,1)\|IMPOUNDMENT CONTAINMENT CAPSULE(14,1)\|LIMIT WATER CONSUMPTION(14,1)\|PROPANE(12,6)\|IMPERMEABLE FLOOR(12,3)\|NEARBY IMPOUNDMENT(12,2)\|TRILLION BARREL(12,2)\|BENTONITE AMENDED SOIL(12,1)\|HYDRO LEAN SHALE(12,1)\|TEXTURED BUILT TAIL BERM(12,1)\|WATER CONSUMPTION(12,1)\|WOVEN BAMBOO BASKET(12,1)\|PEAT(11,4)\|RADIO FREQUENCY(11,3)\|SOIL COMPACTION(11,3)\|IMPERMEABLE SIDEWALL(11,2)\|VOID VOLUME(10,7)\|GUIDELINE(10,4)\|MINED CRUSHED STONE(10,2)\|AVERAGE SIZE(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|COMMINUTED AGGLOMERATE(10,1)\|HEATING(10,1)\|HYDROCARBON LEAN SHALE(10,1)\|IMPOUNDMENT PERIMETER(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|LANDFILL IMPOUNDMENT(10,1)\|LEAK PROOF EXTRACTION IMPOUNDMENT(10,1)\|NANOCARBON FULLERENE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SPRAYED CEMENT SLURRY(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|IMPOUNDMENT HEIGHT(9,2)\|COMPACTED GEOGRID(9,1)\|CONDUIT STRUCTURING(9,1)\|DEBT PAYBACK(9,1)\|ECONOMIC VALUATION(9,1)\|EMPTY IMPOUNDMENT(9,1)\|ENGINEERED CARBON REINFORCED GRID(9,1)\|GASEOUS HYDROCARBON COMBUSTION HEATER(9,1)\|GEOLOGICAL RESERVOIR ANALYSIS(9,1)\|GEOSYNTHETIC FABRICS(9,1)\|GRADE CEMENT SLURRY(9,1)\|HYDROCARBON EXCAVATION(9,1)\|IMPOUNDMENT COLLECTION(9,1)\|IMPOUNDMENT SIDEWALL(9,1)\|INFRASTRUCTURE STABILIZATION(9,1)\|METHANEDIONE RESOLUTION(9,1)\|MINING AVOIDANCE(9,1)\|NEARBY INFRASTRUCTURE(9,1)\|NONCIRCULAR TUBING(9,1)\|PILED RUBBLE(9,1)\|PIT EXCAVATION(9,1)\|REGULATORY FLUID MIGRATION REGULATION(9,1)\|REMAINING SHALE DECREASING WETTABILITY(9,1)\|RESISTANT PVC LINER(9,1)\|THERMALLY DETERIORATED WASTE SHALE(9,1)\|UNCOVERED CAPSULE(9,1)\|UNDERGROUND RUBBLE CHANNEL(9,1)\|UNRECOVERED HYDROCARBON(9,1)\|UNUSED RESOURCE(9,1)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|LIQUID PRODUCT(7,11)\|GASEOUS PRODUCT(7,4)\|CONVECTIVE HEATING(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HORIZONTAL MINING(7,2)\|OIL BLEND(7,2)\|UNCONTROLLED MIGRATION PREVENTION(7,2)\|API MODIFIER(7,1)\|ATMOSPHERIC POLLUTANT(7,1)\|CANADIAN TAR SAND(7,1)\|CARBONATE DECOMPOSITION(7,1)\|CEMENT REINFORCEMENT(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DECREASING HYDROGENATION(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|GEOTEXTILE BAG(7,1)\|GRAVITY ASSISTED DRAIN(7,1)\|GRAVITY DRAINAGE PROFILE(7,1)\|HYDROCARBON ENRICHMENT(7,1)\|HYDROCARBON EXCAVATED VOLUME(7,1)\|HYDROCARBON RICHNESS(7,1)\|HYDROCARBON UNCONTROLLED RELEASE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPERVIOUS BED(7,1)\|IMPOUNDMENT FLOOR(7,1)\|INORGANIC COMPONENT(7,1)\|INSULATION CONTAINMENT(7,1)\|MATERIAL HANDLING COST(7,1)\|MESSY DUMP(7,1)\|MINING HAUL TRUCK(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PLURAL REFERENT(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REGULATORY REGULATION(7,1)\|REINFORCED CEMENT(7,1)\|SHALE MINING(7,1)\|SHELL ICP(7,1)\|SOIL AMENDMENT(7,1)\|SOY INSULATOR(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|USEABLE BODYA GOOD BALANCE(7,1)\|WATERPROOF QUALITY INSULATION(7,1)\|WELLBORE DRILLING(7,1)\|HEAT TRANSFER(6,11)\|HYDROGEN DONOR(6,7)\|COMPACTED FILL TOP(6,3)\|CONVECTION(6,3)\|HEAT PIPE(6,3)\|MINED HYDROCARBONACEOUS MATERIAL(6,3)\|PYROLYSIS(6,3)\|BIOREMEDIATION(6,2)\|GASEOUS LIGHT HYDROCARBON(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|BUILT CAPSULE(6,1)\|CARBON REINFORCING GRID(6,1)\|CERMET COMPOSITE(6,1)\|COLLECTION TROUGH(6,1)\|CONSTRUCTED SULFUR CAPSULE(6,1)\|CONTAINMENT VESSEL SEGMENTATION(6,1)\|CONTAINMENT VESSEL STRUCTURE(6,1)\|DAMAGING STRESS(6,1)\|ECONOMIC FACTOR(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTNESS(6,1)\|ENRICHMENT SENSOR(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|EXTRACTION CAPSULE TREATMENT ZONE(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|FORMATION EXPERIMENTAL MODELING(6,1)\|GEOPOLITICAL FACTOR(6,1)\|HYDROCARBON BEARING(6,1)\|HYDROCARBONACEOUS MATERIAL RESULT(6,1)\|IMMEDIATE INTRODUCTION(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT LIFE SPAN(6,1)\|IMPOUNDMENT REGION(6,1)\|LEACHATE PRODUCTION(6,1)\|LEAK PROOF CONTAINMENT VESSEL(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MAXIMIZE RECOVERY(6,1)\|METHANEDIONE PRODUCTION(6,1)\|MICROBIAL STRAIN(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|OUTER CAPSULE IMPOUNDMENT(6,1)\|PERFORATED HEATING PIPE(6,1)\|PERMEABILITY BARRIER(6,1)\|PERMEABLE PARTICLE(6,1)\|PIPE CONDENSER(6,1)\|PIPE PERFORATION(6,1)\|PREFABRICATED PIECE(6,1)\|PREFORMED PIECE(6,1)\|PROVEN RESERVOIR(6,1)\|RECOVERY STEAM(6,1)\|REDUCING CO2EMISSIONS(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|RESISTIVE HEATER(6,1)\|REUSABLE PIPE(6,1)\|ROTARY RETORT(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STAGED CONTAINMENT VESSEL(6,1)\|STAGING PIPE(6,1)\|SUBTERRANEAN TREATMENT ZONE(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SUPPORTIVE IMPOUNDMENT WALL FORMATION(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANOCARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|TUNNELING(6,1)\|ULTRASONIC GENERATOR(6,1)\|VOLATILE HYDROCARBON(6,1)\|MINED MATERIAL(5,5)\|ENZYME(5,4)\|HEATING RATE(5,4)\|AGITATION(5,3)\|ADJACENT IMPOUNDMENT(5,2)\|ANCHOR MEMBER(5,2)\|ASPHALTENE(5,2)\|CATHETER(5,2)\|COMBUSTION EXHAUST GAS(5,2)\|CRUSHING(5,2)\|CULLET(5,2)\|DETONATION(5,2)\|EXPLOSION(5,2)\|FIBERGLASS(5,2)\|HYDROCARBON LIQUID(5,2)\|HYDROGEN CONTENT(5,2)\|INVESTIGATION(5,2)\|PORTABLE COMBUSTION CHAMBER(5,2)\|PRECIPITATION(5,2)\|RECIRCULATION(5,2)\|SEQUESTRATION(5,2)\|SWELLING(5,2)\|ABUNDANT LIGHT HYDROCARBON(5,1)\|AMBIENT ENVIRONMENT(5,1)\|ANAEROBIC CONDITION(5,1)\|BARRIER MANUFACTURE(5,1)\|BLENDING KEROGEN OIL(5,1)\|CAPACITY INDICATOR(5,1)\|CENTRAL GATHERING PIPE(5,1)\|CHROMATOGRAPHIC LOCATION(5,1)\|COMPLEX MACHINERY(5,1)\|COMPUTER AIDED MINING(5,1)\|COMPUTER EQUIPMENT(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|CONSTRUCTED SULFUR CONTAINMENT VESSEL(5,1)\|CONTAINMENT DISPOSAL AREA(5,1)\|CONTAINMENT VOLUME(5,1)\|COOLING INCREASE(5,1)\|CRUDE EXTRACTION(5,1)\|DECREASING SULFUR(5,1)\|DECREASING VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|ENCAPSULATED IMPOUNDMENT AREA(5,1)\|ENRICHED OIL BEARING ORE(5,1)\|EXPOSED UNDISTURBED GROUND(5,1)\|EXTRACTION PORT(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLOOR CONSTRUCTION(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GEOLOGICAL LOCATION(5,1)\|HORIZONTAL BOREHOLE(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBON VAPOR(5,1)\|HYDROCARBONACEOUS MATERIAL BIOHYDROXYLATION(5,1)\|INFRASTRUCTURE LOCATION(5,1)\|INORGANIC MATTER(5,1)\|ION RESIN EXCHANGE(5,1)\|KEROGEN REMOVAL(5,1)\|LARGE CONTAINMENT IMPOUNDMENT(5,1)\|LAYER COMPACTION(5,1)\|LOCALIZED HEATING ZONE(5,1)\|METEOROLOGICAL DATA FACTOR(5,1)\|MINIMAL WASTE(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONHYDROCARBON(5,1)\|NONOXIDIZING GAS(5,1)\|OIL SHALE ORE(5,1)\|OPEN ENDED CAPSULE IMPOUNDMENT(5,1)\|OPTIMIZATION REASON(5,1)\|PATHWAY(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PREVENT ACCIDENTAL LEACHING(5,1)\|PREVENTION MEASURE(5,1)\|PUMPING PIPE(5,1)\|PURGE GAS(5,1)\|RECOVERING OIL(5,1)\|RECUPERATOR(5,1)\|REFORMATION(5,1)\|RELEVANT MEASUREMENT(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RETURN DILUENT(5,1)\|ROUND TUBING(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|SPRAYED LIQUID EMULSION(5,1)\|STAGED PROCESSING(5,1)\|STEEL RETORT(5,1)\|STRUCTURED FEATURE(5,1)\|SUPPLEMENTAL HEATING(5,1)\|SUPPORTING BERM(5,1)\|TECHNICAL CHALLENGE(5,1)\|TRANSFER DEFLATION(5,1)\|TRANSPORT CONDUIT(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNDERGROUND AQUIFER(5,1)\|UPGRADING(5,1)\|VOLATILE ORGANIC(5,1)\|WATERTIGHT COVER(5,1)\|HEATED FLUID(4,3)\|INJECTION RATE(4,3)\|SILO(4,3)\|VAPOR PRODUCTION(4,2)\|ACROSS MULTIPLE IMPOUNDMENT(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADVENT(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALONE MEET(3,1)\|ANCHOR PILE STRUCTURE(3,1)\|AQUEOUS MUD CONDITION(3,1)\|AROMATICS(3,1)\|ASSAYING(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOGLASS(3,1)\|BIOLEACHING(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CATALYTIC GAS(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|CENTRAL RESERVOIR(3,1)\|COAL COMBINATION(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONCENTRATE(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED GEOMEMBRANE LAYER(3,1)\|CONTAINMENT CONSTRUCTION(3,1)\|CONTAINMENT VESSEL CONSTRUCTION(3,1)\|CONTOUR(3,1)\|CONTROLLED QUALITY SHALE(3,1)\|COOLING FLUID(3,1)\|COOLING PIPE(3,1)\|CURRENCY(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DEADMAN(3,1)\|DOWNWARDLY TRANSFERRED LIQUID(3,1)\|DUMPING(3,1)\|EARTH FORMATION(3,1)\|ELECTRICITY(3,1)\|ELECTROLYTE(3,1)\|ELECTROPLATING(3,1)\|ELEVATOR(3,1)\|ENHANCE REMOVAL(3,1)\|ENHANCER(3,1)\|ESTIMATE SOURCE(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLEXIBLE HOUSING(3,1)\|FLOTATION(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID EXTRACTION(3,1)\|FRACTURE(3,1)\|FRACTURING(3,1)\|FUNCTIONAL VOID SPACE(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS COMBUSTION(3,1)\|GAS GATHERING(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GAS RELEASE(3,1)\|GEOSYNTHETIC MEMBRANE(3,1)\|GRADE PLANE(3,1)\|HALF ACRE(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HAULING(3,1)\|HEAT ABSORPTION(3,1)\|HEATING CONDUIT COST(3,1)\|HEATING CONDUIT LOCATION(3,1)\|HEATING FLUID ISOLATION(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTRATION(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBONACEOUS MATERIAL COMPACTION(3,1)\|HYDROTREAT(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE BOTTOM(3,1)\|\|(CN102395653)\|HYDROCARBONACEOUS MATERIAL(100,46)\|INFRASTRUCTURE CONSTRUCTION(100,23)\|INFRASTRUCTURE(100,21)\|POSITIVE PRESSURE(100,15)\|CONSTRUCTED PERMEABILITY(100,12)\|RECOVERING HYDROCARBON(100,11)\|ENCAPSULATED VOLUME(94,19)\|ECONOMICALLY COMPETITIVE RECOVERY(84,1)\|UNDERGROUND AQUIFER CONTAMINATION(75,1)\|DIRTY FINE PARTICULATE(71,1)\|GASEOUS FLUID(70,5)\|BENTONITE CLAY(64,1)\|GASEOUS COMPONENT(61,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(58,6)\|CLAY LINING(56,1)\|IMPOUNDMENT(46,63)\|SYNTHETIC CLAY(46,1)\|FLUSH HYDROCARBON VAPOR(43,1)\|DRAINAGE PIPE(42,2)\|CONTROL INFRASTRUCTURE(41,21)\|ECONOMICS(40,1)\|TEMPERATURE GEOMEMBRANE(40,1)\|UNDESIRED HYDROCARBON(40,1)\|DIFFICULT CHALLENGE(39,1)\|BRINE SOLUTION(36,1)\|HYDROCARBON RESIDUE(34,1)\|SOLVENT RECOVERY(33,2)\|OBSERVABLE(33,1)\|IMPOUNDMENT WALL(32,11)\|PERMEABILITY CONTROL IMPOUNDMENT(32,3)\|ASSURANCE(32,1)\|ENVIRONMENTAL HAZARD(32,1)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(32,1)\|SEALANT(32,1)\|REMEDIATION(31,2)\|ENCLOSED VOLUME(29,7)\|UNDERGROUND MINING(28,2)\|SEGMENTED CAPSULE IMPOUNDMENT(27,3)\|BRINE(26,1)\|VOID SPACE(25,5)\|FREEZE WALL(25,3)\|GASEOUS MATERIAL(25,3)\|BLASTING(25,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(24,1)\|LEAK(24,1)\|HYDROCARBON MATERIAL FLUSHING(23,1)\|OUTPUT CAPACITY(23,1)\|REMOVING PRODUCT(23,1)\|REFRACTORY CEMENT(22,4)\|BIOMASS(22,3)\|REMOVING HYDROCARBON(22,3)\|ADDITIVE(20,14)\|GRAVEL(20,3)\|REBAR(20,3)\|STOICHIOMETRIC CONDITION(20,3)\|TOTAL VOLUME(20,2)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(20,1)\|PREVENTABLE WATER BODY(20,1)\|GROUT(19,3)\|ADAPTABLE WATER BODY(18,1)\|SURFACE DISTURBANCE(18,1)\|UNDERGROUND FRESHWATER AQUIFER(18,1)\|LIGNITE(17,4)\|BIOCHEMICALLY OXIDIZE ORE(17,1)\|HEATED HYDROCARBONACEOUS MATERIAL(17,1)\|MINE CAPSULE IMPOUNDMENT(17,1)\|WATER POLLUTION(17,1)\|AFT BERM PERMEABILITY(16,1)\|IMPOUNDMENT CONTAINMENT CAPSULE(16,1)\|LIMIT WATER CONSUMPTION(16,1)\|HYDROCARBON PRODUCTION(15,12)\|IMPERMEABLE FLOOR(14,3)\|NEARBY IMPOUNDMENT(14,2)\|TRILLION BARREL(14,2)\|BENTONITE AMENDED SOIL(14,1)\|HYDRO LEAN SHALE(14,1)\|WATER CONSUMPTION(14,1)\|WOVEN BAMBOO BASKET(14,1)\|PROPANE(13,6)\|PEAT(13,4)\|RADIO FREQUENCY(13,3)\|IMPERMEABLE SIDEWALL(13,2)\|VOID VOLUME(12,7)\|SOIL COMPACTION(12,3)\|MINED CRUSHED STONE(12,2)\|GUIDELINE(11,4)\|AVERAGE SIZE(11,1)\|BIOEXTRACTION SCENARIO(11,1)\|CHALLENGING ENDEAVOR(11,1)\|COLLECTIVE IMPOUNDMENT(11,1)\|COMMINUTED AGGLOMERATE(11,1)\|HEATING(11,1)\|HYDROCARBON LEAN SHALE(11,1)\|IMPOUNDMENT PERIMETER(11,1)\|INFRASTRUCTURE SHUTDOWN(11,1)\|LANDFILL IMPOUNDMENT(11,1)\|LEAK PROOF EXTRACTION IMPOUNDMENT(11,1)\|NANOCARBON FULLERENE(11,1)\|SEWAGE IMPOUNDMENT(11,1)\|SPRAYED CEMENT SLURRY(11,1)\|SUBDIVIDED IMPOUNDMENT(11,1)\|WATERPROOF QUALITY ENGINEERING(11,1)\|UNDISTURBED GEOLOGICAL FORMATION(10,3)\|IMPOUNDMENT HEIGHT(10,2)\|COMPACTED GEOGRID(10,1)\|CONDUIT STRUCTURING(10,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(10,1)\|DEBT PAYBACK(10,1)\|ECONOMIC VALUATION(10,1)\|EMPTY IMPOUNDMENT(10,1)\|ENGINEERED CARBON REINFORCED GRID(10,1)\|GASEOUS HYDROCARBON COMBUSTION HEATER(10,1)\|GEOLOGICAL RESERVOIR ANALYSIS(10,1)\|GEOSYNTHETIC FABRICS(10,1)\|GRADE CEMENT SLURRY(10,1)\|HYDROCARBON EXCAVATION(10,1)\|IMPOUNDMENT COLLECTION(10,1)\|IMPOUNDMENT SIDEWALL(10,1)\|INFRASTRUCTURE STABILIZATION(10,1)\|METHANEDIONE RESOLUTION(10,1)\|MINING AVOIDANCE(10,1)\|NEARBY INFRASTRUCTURE(10,1)\|NONCIRCULAR TUBING(10,1)\|PILED RUBBLE(10,1)\|PIT EXCAVATION(10,1)\|REGULATORY FLUID MIGRATION REGULATION(10,1)\|REMAINING SHALE DECREASING WETTABILITY(10,1)\|RESISTANT PVC LINER(10,1)\|TEXTURED BUILT TAIL(10,1)\|THERMALLY DETERIORATED WASTE SHALE(10,1)\|UNCOVERED CAPSULE(10,1)\|UNDERGROUND RUBBLE CHANNEL(10,1)\|UNRECOVERED HYDROCARBON(10,1)\|UNUSED RESOURCE(10,1)\|LIQUID PRODUCT(8,11)\|GASEOUS PRODUCT(8,4)\|CONVECTIVE HEATING(8,2)\|HORIZONTAL MINING(8,2)\|OIL BLEND(8,2)\|UNCONTROLLED MIGRATION PREVENTION(8,2)\|API MODIFIER(8,1)\|ATMOSPHERIC POLLUTANT(8,1)\|CANADIAN TAR SAND(8,1)\|CARBONATE DECOMPOSITION(8,1)\|CEMENT REINFORCEMENT(8,1)\|CONTAINMENT BOUNDARY(8,1)\|CRANE SUSPENDED EXCAVATOR(8,1)\|CRUSHED ORE(8,1)\|DECREASING HYDROGENATION(8,1)\|ECONOMIC OPPORTUNITY(8,1)\|EXCAVATED CAVITY(8,1)\|GEOTEXTILE BAG(8,1)\|GRAVITY ASSISTED DRAIN(8,1)\|GRAVITY DRAINAGE PROFILE(8,1)\|HYDROCARBON ENRICHMENT(8,1)\|HYDROCARBON EXCAVATED VOLUME(8,1)\|HYDROCARBON RICHNESS(8,1)\|HYDROCARBON UNCONTROLLED RELEASE(8,1)\|IMPERMEABLE BARRIER ZONE(8,1)\|IMPERVIOUS BED(8,1)\|IMPOUNDMENT FLOOR(8,1)\|INORGANIC COMPONENT(8,1)\|INSULATION CONTAINMENT(8,1)\|MATERIAL HANDLING COST(8,1)\|MESSY DUMP(8,1)\|MINING HAUL TRUCK(8,1)\|NATIVE BACTERIA(8,1)\|NATURAL DISTRIBUTED COMBUSTOR(8,1)\|ORE SOLVENT EXTRACTION(8,1)\|PILLAR MINING(8,1)\|PLURAL REFERENT(8,1)\|REFORMING CATALYST(8,1)\|REFORMING ZONE(8,1)\|REGULATORY REGULATION(8,1)\|REINFORCED CEMENT(8,1)\|SHALE MINING(8,1)\|SHELL ICP(8,1)\|SOIL AMENDMENT(8,1)\|SOY INSULATOR(8,1)\|STOICHIOMETRIC COMBUSTION(8,1)\|SUPER DISPOSITION(8,1)\|TAR SAND BITUMEN TREATMENT(8,1)\|WATERPROOF QUALITY INSULATION(8,1)\|WELLBORE DRILLING(8,1)\|HEAT TRANSFER(7,11)\|HYDROGEN DONOR(7,7)\|CONVECTION(7,3)\|HEAT PIPE(7,3)\|MINED HYDROCARBONACEOUS MATERIAL(7,3)\|PYROLYSIS(7,3)\|BIOREMEDIATION(7,2)\|GASEOUS LIGHT HYDROCARBON(7,2)\|ACCEPTED PIPELINE STANDARD(7,1)\|BUILT CAPSULE(7,1)\|CARBON REINFORCING GRID(7,1)\|CERMET COMPOSITE(7,1)\|COLLECTION TROUGH(7,1)\|CONSTRUCTED SULFUR CAPSULE(7,1)\|CONTAINMENT VESSEL SEGMENTATION(7,1)\|CONTAINMENT VESSEL STRUCTURE(7,1)\|DAMAGING STRESS(7,1)\|ECONOMIC FACTOR(7,1)\|EMBEDDED CONDUIT(7,1)\|ENHANCE COMPACTNESS(7,1)\|ENRICHMENT SENSOR(7,1)\|EXPLICITLY RECITED LIMIT(7,1)\|EXTRACTION CAPSULE TREATMENT ZONE(7,1)\|FLOOR LEVELING(7,1)\|FLUSH HYDROCARBON(7,1)\|FORMATION EXPERIMENTAL MODELING(7,1)\|GEOPOLITICAL FACTOR(7,1)\|HYDROCARBON BEARING(7,1)\|HYDROCARBONACEOUS MATERIAL RESULT(7,1)\|IMMEDIATE INTRODUCTION(7,1)\|IMPOUNDMENT DEPTH(7,1)\|IMPOUNDMENT LIFE SPAN(7,1)\|IMPOUNDMENT REGION(7,1)\|LEACHATE PRODUCTION(7,1)\|LEAK PROOF CONTAINMENT VESSEL(7,1)\|LOCALIZED HOTSPOT ELIMINATION(7,1)\|MAXIMIZE RECOVERY(7,1)\|METHANEDIONE PRODUCTION(7,1)\|MICROBIAL STRAIN(7,1)\|MINERAL LINER(7,1)\|MINING ORE GRADE(7,1)\|MOISTURE MIGRATION(7,1)\|ORE MOISTURE CONTENT(7,1)\|OUTER CAPSULE IMPOUNDMENT(7,1)\|PERFORATED HEATING PIPE(7,1)\|PERMEABILITY BARRIER(7,1)\|PERMEABLE PARTICLE(7,1)\|PIPE CONDENSER(7,1)\|PIPE PERFORATION(7,1)\|PREFABRICATED PIECE(7,1)\|PREFORMED PIECE(7,1)\|PROVEN RESERVOIR(7,1)\|RECOVERY STEAM(7,1)\|REDUCING CO2EMISSIONS(7,1)\|REFRACTORY CEMENT PIPE(7,1)\|RESISTIVE HEATER(7,1)\|REUSABLE PIPE(7,1)\|ROTARY RETORT(7,1)\|SPENT SHALE SOLID RINSING(7,1)\|STAGED CONTAINMENT VESSEL(7,1)\|STAGING PIPE(7,1)\|SUBTERRANEAN TREATMENT ZONE(7,1)\|SUPPLEMENTAL FUEL(7,1)\|SUPPORTIVE IMPOUNDMENT WALL FORMATION(7,1)\|SYNTHETIC GEOGRID(7,1)\|SYNTHETIC NANOCARBON(7,1)\|TAR SAND DEPOSIT(7,1)\|TOXIC EFFLUENT(7,1)\|TUNNELING(7,1)\|ULTRASONIC GENERATOR(7,1)\|VOLATILE HYDROCARBON(7,1)\|CLAY(6,5)\|MINED MATERIAL(6,5)\|ENZYME(6,4)\|AGITATION(6,3)\|ADJACENT IMPOUNDMENT(6,2)\|ANCHOR MEMBER(6,2)\|ASPHALTENE(6,2)\|CATHETER(6,2)\|COMBUSTION EXHAUST GAS(6,2)\|COMPACTED FILL TOP(6,2)\|CRUSHING(6,2)\|CULLET(6,2)\|DETONATION(6,2)\|EXPLOSION(6,2)\|FIBERGLASS(6,2)\|HYDROCARBON LIQUID(6,2)\|HYDROGEN CONTENT(6,2)\|INVESTIGATION(6,2)\|PORTABLE COMBUSTION CHAMBER(6,2)\|PRECIPITATION(6,2)\|RECIRCULATION(6,2)\|SEQUESTRATION(6,2)\|SWELLING(6,2)\|HEATING RATE(5,4)\|HEATED FLUID(5,3)\|INJECTION RATE(5,3)\|SILO(5,3)\|VAPOR PRODUCTION(5,2)\|ABUNDANT LIGHT HYDROCARBON(5,1)\|AMBIENT ENVIRONMENT(5,1)\|ANAEROBIC CONDITION(5,1)\|BARRIER MANUFACTURE(5,1)\|BLENDING KEROGEN OIL(5,1)\|CAPACITY INDICATOR(5,1)\|CENTRAL GATHERING PIPE(5,1)\|CHROMATOGRAPHIC LOCATION(5,1)\|COMPLEX MACHINERY(5,1)\|COMPUTER AIDED MINING(5,1)\|COMPUTER EQUIPMENT(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|CONSTRUCTED SULFUR CONTAINMENT VESSEL(5,1)\|CONTAINMENT DISPOSAL AREA(5,1)\|CONTAINMENT VOLUME(5,1)\|COOLING INCREASE(5,1)\|CRUDE EXTRACTION(5,1)\|DECREASING SULFUR(5,1)\|DECREASING VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|ENCAPSULATED IMPOUNDMENT AREA(5,1)\|ENRICHED OIL BEARING ORE(5,1)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(5,1)\|EXPOSED UNDISTURBED GROUND(5,1)\|EXTRACTION PORT(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLOOR CONSTRUCTION(5,1)\|GAS OXIDATION(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GEOLOGICAL LOCATION(5,1)\|HORIZONTAL BOREHOLE(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBON VAPOR(5,1)\|HYDROCARBONACEOUS MATERIAL BIOHYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|INFRASTRUCTURE LOCATION(5,1)\|INORGANIC MATTER(5,1)\|ION RESIN EXCHANGE(5,1)\|KEROGEN REMOVAL(5,1)\|LARGE CONTAINMENT IMPOUNDMENT(5,1)\|LAYER COMPACTION(5,1)\|LOCALIZED HEATING ZONE(5,1)\|METEOROLOGICAL DATA FACTOR(5,1)\|MINIMAL WASTE(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONHYDROCARBON(5,1)\|NONOXIDIZING GAS(5,1)\|OIL SHALE ORE(5,1)\|OPEN ENDED CAPSULE IMPOUNDMENT(5,1)\|OPTIMIZATION REASON(5,1)\|PATHWAY(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PREVENT ACCIDENTAL LEACHING(5,1)\|PREVENTION MEASURE(5,1)\|PROBLEMSAND(5,1)\|PUMPING PIPE(5,1)\|PURGE GAS(5,1)\|RECOVERING OIL(5,1)\|RECUPERATOR(5,1)\|REFORMATION(5,1)\|RELEVANT MEASUREMENT(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RETURN DILUENT(5,1)\|ROUND TUBING(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|SPRAYED LIQUID EMULSION(5,1)\|STAGED PROCESSING(5,1)\|STEEL RETORT(5,1)\|STRUCTURED FEATURE(5,1)\|SUPPLEMENTAL HEATING(5,1)\|SUPPORTING BERMS(5,1)\|TECHNICAL CHALLENGE(5,1)\|TRANSFER DEFLATION(5,1)\|TRANSPORT CONDUIT(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNDERGROUND AQUIFER(5,1)\|UPGRADING(5,1)\|VOLATILE ORGANIC(5,1)\|WATERTIGHT COVER(5,1)\|ACROSS MULTIPLE IMPOUNDMENT(4,1)\|ADJACENT INFRASTRUCTURE(4,1)\|ADVENT(4,1)\|AGGREGATE PRODUCTION(4,1)\|ALONE MEET(4,1)\|ANCHOR PILE STRUCTURE(4,1)\|AQUEOUS MUD CONDITION(4,1)\|AROMATICS(4,1)\|ASSAYING(4,1)\|AVAILABLE ADDRESSING(4,1)\|BAUXITE(4,1)\|BINDER(4,1)\|BIOCATALYST(4,1)\|BIOGLASS(4,1)\|BIOLEACHING(4,1)\|BITUMEN SOURCE(4,1)\|CALCINED PETROLEUM COKE(4,1)\|CATALYTIC GAS(4,1)\|CATALYTICALLY ACTIVE METAL(4,1)\|CENTRAL RESERVOIR(4,1)\|COAL COMBINATION(4,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(4,1)\|COMPOSITE WALL(4,1)\|COMPOUND SUBSTITUTION(4,1)\|CONCENTRATE(4,1)\|CONDENSABILITY(4,1)\|CONDUIT PASS(4,1)\|CONDUIT WALL(4,1)\|CONSTRUCTED GEOMEMBRANE LAYER(4,1)\|CONTAINMENT CONSTRUCTION(4,1)\|CONTAINMENT VESSEL CONSTRUCTION(4,1)\|CONTOUR(4,1)\|CONTROLLED QUALITY SHALE(4,1)\|COOLING FLUID(4,1)\|COOLING PIPE(4,1)\|CURRENCY(4,1)\|CYCLOHEXANE(4,1)\|CYCLOPENTANE(4,1)\|DEADMAN(4,1)\|DICTATION(4,1)\|DOWNWARDLY TRANSFERRED LIQUID(4,1)\|DUMPING(4,1)\|EARTH FORMATION(4,1)\|ELECTRICITY(4,1)\|ELECTROLYTE(4,1)\|ELECTROPLATING(4,1)\|ELEVATOR(4,1)\|ENHANCE REMOVAL(4,1)\|ENHANCER(4,1)\|ESTIMATE SOURCE(4,1)\|EXCAVATION AREA(4,1)\|FINAL HYDROCARBON PRODUCT(4,1)\|FINAL PRODUCT RECOVERY(4,1)\|FINE MESH(4,1)\|FLEXIBLE HOUSING(4,1)\|FLOTATION(4,1)\|FLUID COMMUNICATION(4,1)\|FLUID EXTRACTION(4,1)\|FRACTURE(4,1)\|FRACTURING(4,1)\|FUNCTIONAL VOID SPACE(4,1)\|GAS BARRIER(4,1)\|GAS COLLECTION OUTLET(4,1)\|GAS COMBUSTION(4,1)\|GAS GATHERING(4,1)\|GAS INJECTION(4,1)\|GAS MIGRATION(4,1)\|GAS RELEASE(4,1)\|GEOSYNTHETIC MEMBRANE(4,1)\|GRADE PLANE(4,1)\|HALF ACRE(4,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(4,1)\|HAULING(4,1)\|HEAT ABSORPTION(4,1)\|HEATING CONDUIT COST(4,1)\|HEATING CONDUIT LOCATION(4,1)\|HEATING FLUID ISOLATION(4,1)\|HOLDING TANK PROXIMITY(4,1)\|HOT GAS FILTRATION(4,1)\|HYDROCARBON GAS(4,1)\|HYDROCARBONACEOUS MATERIAL COMPACTION(4,1)\|HYDROTREAT(4,1)\|\|(AU2010213774)\|HYDROCARBONACEOUS MATERIAL(100,45)\|INFRASTRUCTURE(100,23)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,17)\|CONSTRUCTED PERMEABILITY(100,13)\|RECOVERING HYDROCARBON(100,13)\|ENCAPSULATED VOLUME(93,29)\|GASEOUS FLUID(52,6)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(48,6)\|GASEOUS COMPONENT(39,4)\|CONTROL INFRASTRUCTURE(37,25)\|FLUSH RESIDUAL HYDROCARBON(37,1)\|FLUSH HYDROCARBON VAPOR(36,1)\|COLLECTING REMOVED HYDROCARBON(27,2)\|HYDROCARBON COMBUSTION(26,2)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(26,1)\|PERMEABILITY CONTROL IMPOUNDMENT(25,4)\|HYDROCARBONACEOUS MATERIAL FLUSHING(25,1)\|GASEOUS MATERIAL(20,3)\|HEATED HYDROCARBONACEOUS MATERIAL(20,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(20,1)\|VOID SPACE(19,5)\|MALFUNCTION(19,1)\|SECTIONED CAPSULE IMPOUNDMENT(18,2)\|STOICHIOMETRIC CONDITION(18,2)\|COMPACTED FILL CEILING(16,3)\|TOTAL VOLUME(16,2)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(16,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(15,1)\|UNDERGROUND FRESHWATER AQUIFER(15,1)\|LIGNITE(14,4)\|QUARRY CAPSULE IMPOUNDMENT(14,1)\|UNCAPPED CAPSULE IMPOUNDMENT(14,1)\|UNDERGROUND RUBBLE CHIMNEY(14,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(13,1)\|NANOCARBON FULLERENE ADDITIVE(13,1)\|STRUCTURED IMPOUNDMENT CAPSULE(13,1)\|HYDROCARBON PRODUCTION(12,11)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|PROPANE(11,6)\|CONTAINMENT CAPSULE(11,2)\|NEARBY IMPOUNDMENT(11,2)\|TAILING BERM(11,2)\|UNRECOVERED HYDROCARBON(11,2)\|COAL(10,7)\|PEAT(10,4)\|BENTONITE CLAY(10,2)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|ENGINEERED PERMEABILITY BARRIER(10,1)\|HYDROCARBON UNCONTROLLED EGRESS(10,1)\|UNDERGROUND MINED HYDROCARBON(10,1)\|BENCH MINING ELEVATION(9,1)\|BIOEXTRACTION SCENARIO(9,1)\|CHALLENGING ENDEAVOR(9,1)\|COLLECTIVE IMPOUNDMENT(9,1)\|EXTERIOR CAPSULE IMPOUNDMENT(9,1)\|GARBAGE IMPOUNDMENT(9,1)\|GRAVITY ASSISTED DRAINAGE PIPE(9,1)\|GRAVITY DRAINAGE ASSISTANCE(9,1)\|INDISCRIMINATE DUMPING(9,1)\|INFRASTRUCTURE SHUTDOWN(9,1)\|MANIPULATED GRADE SHALE(9,1)\|MEDIAN SIZE(9,1)\|SEWAGE IMPOUNDMENT(9,1)\|SUBDIVIDED IMPOUNDMENT(9,1)\|UNTAPPED RESOURCE(9,1)\|WATERPROOF QUALITY ENGINEERING(9,1)\|HEAT PIPE(8,6)\|GUIDELINE(8,3)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CONSTRUCTED SULFUR CAPSULE(8,2)\|IMPOUNDMENT HEIGHT(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MILLING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|VOID VOLUME(7,4)\|CORE DRILLING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|LEAN SHALE(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|LIQUID PRODUCT(6,10)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|CONVECTIVE HEATING(6,2)\|CRUSHED GLASS(6,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(6,2)\|HEATED CONDUIT(6,2)\|HEATING(6,2)\|HORIZONTAL MINING(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|CARBONATE DECOMPOSITION(6,1)\|CO2 EMISSION(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|HYDROGEN DONOR(5,6)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|ANTHEM DEGREE(5,2)\|BLASTING(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|FLOOR CONSTRUCTION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|KEROGEN OIL(4,4)\|HEATED FLUID(4,3)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|PIPING(4,3)\|ANAEROBIC CONDITION(4,1)\|AQUEOUS SLURRY(4,1)\|BARRIER MANUFACTURE(4,1)\|CAPACITY INDICATOR(4,1)\|CAPSULE IMPOUNDMENT AREA(4,1)\|CATALYZING GAS(4,1)\|CEILING CAP(4,1)\|CLAY PIPE(4,1)\|COMMINUTED MASS(4,1)\|COMPOSITION ADMIXTURE(4,1)\|CONCRETE PANEL(4,1)\|CONDUCTIVE CEMENT(4,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(4,1)\|CONSTRUCTED IMPOUNDMENT(4,1)\|DECREASED VISCOSITY(4,1)\|DISPERSION FLUID SENSOR(4,1)\|DUST PARTICLE(4,1)\|ECONOMICALLY VIABLE SOURCE(4,1)\|FAST RECOVERY(4,1)\|FINE COLLECTION(4,1)\|FLUID DRAINAGE(4,1)\|FLUSHING GAS(4,1)\|GAS COMBUSTION HEATER(4,1)\|GASEOUS HYDROCARBON PRODUCT(4,1)\|GEO MEMBRANE LAYER(4,1)\|GEO SYNTHETIC MEMBRANE(4,1)\|GEOLOGICAL LOCATION(4,1)\|HEATING CONDUIT PLACEMENT(4,1)\|HOTSPOT LOCALIZATION(4,1)\|HYDROCARBON VAPOR(4,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(4,1)\|HYDRODESULFURIZATION(4,1)\|IMPOUNDMENT USEFUL LIFE(4,1)\|INORGANIC MATTER(4,1)\|KEROGEN REMOVAL(4,1)\|LAYER COMPACTION(4,1)\|MICROBIOLOGY(4,1)\|MINIMAL WASTE(4,1)\|MINING HAUL TRUCK NEED(4,1)\|MOLTEN CARBONATE FUEL CELL(4,1)\|MONITORING HEAT(4,1)\|NONHEATED BUFFER ZONE(4,1)\|NONOXIDIZING GAS(4,1)\|OIL BLEND(4,1)\|OPTIMIZATION REASON(4,1)\|PIPELINE EXTENSION(4,1)\|PLANT FIBER CELLULOSE(4,1)\|POLYMERIC RESIN(4,1)\|PRECAST PIECE(4,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(4,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(4,1)\|QUALITY DETERIORATION(4,1)\|RECOVERED HYDROCARBON LIQUID(4,1)\|RECOVERING OIL(4,1)\|REFORMATION(4,1)\|RESIDUAL HYDROCARBON PRODUCT(4,1)\|RESIDUAL SHALE REDUCED WETTING(4,1)\|RICH OIL BEARING ORE(4,1)\|ROTATING RETORT(4,1)\|SAND PARTICLE(4,1)\|SEQUENTIAL SOLUTION RECOVERY(4,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(4,1)\|SOLVENT SUBSTITUTED COMPOUND(4,1)\|STAGED PROCESSING(4,1)\|STEAM INJECTION(4,1)\|TECHNICAL CHALLENGE(4,1)\|TREMENDOUS VOLUME(4,1)\|UNCONTROLLED ESCAPE PREVENTION(4,1)\|UNCONTROLLED MIGRATION PREVENTION(4,1)\|VAPOROUS COMPONENT(4,1)\|VARIED ENZYME(4,1)\|VOLATILE ORGANIC(4,1)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOLEACHING(3,1)\|BIOMATERIAL(3,1)\|BIOOXIDATION(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ECONOMICS(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|EXCLUSION(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCLUSION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|LAYER CONDUIT(3,1)\|LAYING WIRE(3,1)\|LIGHTER(3,1)\|LIMITED COMBUSTION INTENT(3,1)\|LIQUID CONDENSATION(3,1)\|LIQUID EMULSION(3,1)\|LUBRICANT COOLANT(3,1)\|\|(AU2010213774)\|HYDROCARBONACEOUS MATERIAL(100,45)\|INFRASTRUCTURE(100,23)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,17)\|CONSTRUCTED PERMEABILITY(100,13)\|RECOVERING HYDROCARBON(100,13)\|ENCAPSULATED VOLUME(93,29)\|GASEOUS FLUID(52,6)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(48,6)\|GASEOUS COMPONENT(39,4)\|CONTROL INFRASTRUCTURE(37,25)\|FLUSH RESIDUAL HYDROCARBON(37,1)\|FLUSH HYDROCARBON VAPOR(36,1)\|COLLECTING REMOVED HYDROCARBON(27,2)\|HYDROCARBON COMBUSTION(26,2)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(26,1)\|PERMEABILITY CONTROL IMPOUNDMENT(25,4)\|HYDROCARBONACEOUS MATERIAL FLUSHING(25,1)\|GASEOUS MATERIAL(20,3)\|HEATED HYDROCARBONACEOUS MATERIAL(20,2)\|CRUSHED HYDROCARBONACEOUS MATERIAL(20,1)\|VOID SPACE(19,5)\|MALFUNCTION(19,1)\|SECTIONED CAPSULE IMPOUNDMENT(18,2)\|STOICHIOMETRIC CONDITION(18,2)\|COMPACTED FILL CEILING(16,3)\|TOTAL VOLUME(16,2)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(16,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(15,1)\|UNDERGROUND FRESHWATER AQUIFER(15,1)\|LIGNITE(14,4)\|QUARRY CAPSULE IMPOUNDMENT(14,1)\|UNCAPPED CAPSULE IMPOUNDMENT(14,1)\|UNDERGROUND RUBBLE CHIMNEY(14,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(13,1)\|NANOCARBON FULLERENE ADDITIVE(13,1)\|STRUCTURED IMPOUNDMENT CAPSULE(13,1)\|HYDROCARBON PRODUCTION(12,11)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|PROPANE(11,6)\|CONTAINMENT CAPSULE(11,2)\|NEARBY IMPOUNDMENT(11,2)\|TAILING BERM(11,2)\|UNRECOVERED HYDROCARBON(11,2)\|COAL(10,7)\|PEAT(10,4)\|BENTONITE CLAY(10,2)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|ENGINEERED PERMEABILITY BARRIER(10,1)\|HYDROCARBON UNCONTROLLED EGRESS(10,1)\|UNDERGROUND MINED HYDROCARBON(10,1)\|BENCH MINING ELEVATION(9,1)\|BIOEXTRACTION SCENARIO(9,1)\|CHALLENGING ENDEAVOR(9,1)\|COLLECTIVE IMPOUNDMENT(9,1)\|EXTERIOR CAPSULE IMPOUNDMENT(9,1)\|GARBAGE IMPOUNDMENT(9,1)\|GRAVITY ASSISTED DRAINAGE PIPE(9,1)\|GRAVITY DRAINAGE ASSISTANCE(9,1)\|INDISCRIMINATE DUMPING(9,1)\|INFRASTRUCTURE SHUTDOWN(9,1)\|MANIPULATED GRADE SHALE(9,1)\|MEDIAN SIZE(9,1)\|SEWAGE IMPOUNDMENT(9,1)\|SUBDIVIDED IMPOUNDMENT(9,1)\|UNTAPPED RESOURCE(9,1)\|WATERPROOF QUALITY ENGINEERING(9,1)\|HEAT PIPE(8,6)\|GUIDELINE(8,3)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CONSTRUCTED SULFUR CAPSULE(8,2)\|IMPOUNDMENT HEIGHT(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MILLING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|VOID VOLUME(7,4)\|CORE DRILLING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|LEAN SHALE(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|LIQUID PRODUCT(6,10)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|CONVECTIVE HEATING(6,2)\|CRUSHED GLASS(6,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(6,2)\|HEATED CONDUIT(6,2)\|HEATING(6,2)\|HORIZONTAL MINING(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|CARBONATE DECOMPOSITION(6,1)\|CO2 EMISSION(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|HYDROGEN DONOR(5,6)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|ANTHEM DEGREE(5,2)\|BLASTING(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|FLOOR CONSTRUCTION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|KEROGEN OIL(4,4)\|HEATED FLUID(4,3)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|PIPING(4,3)\|ANAEROBIC CONDITION(4,1)\|AQUEOUS SLURRY(4,1)\|BARRIER MANUFACTURE(4,1)\|CAPACITY INDICATOR(4,1)\|CAPSULE IMPOUNDMENT AREA(4,1)\|CATALYZING GAS(4,1)\|CEILING CAP(4,1)\|CLAY PIPE(4,1)\|COMMINUTED MASS(4,1)\|COMPOSITION ADMIXTURE(4,1)\|CONCRETE PANEL(4,1)\|CONDUCTIVE CEMENT(4,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(4,1)\|CONSTRUCTED IMPOUNDMENT(4,1)\|DECREASED VISCOSITY(4,1)\|DISPERSION FLUID SENSOR(4,1)\|DUST PARTICLE(4,1)\|ECONOMICALLY VIABLE SOURCE(4,1)\|FAST RECOVERY(4,1)\|FINE COLLECTION(4,1)\|FLUID DRAINAGE(4,1)\|FLUSHING GAS(4,1)\|GAS COMBUSTION HEATER(4,1)\|GASEOUS HYDROCARBON PRODUCT(4,1)\|GEO MEMBRANE LAYER(4,1)\|GEO SYNTHETIC MEMBRANE(4,1)\|GEOLOGICAL LOCATION(4,1)\|HEATING CONDUIT PLACEMENT(4,1)\|HOTSPOT LOCALIZATION(4,1)\|HYDROCARBON VAPOR(4,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(4,1)\|HYDRODESULFURIZATION(4,1)\|IMPOUNDMENT USEFUL LIFE(4,1)\|INORGANIC MATTER(4,1)\|KEROGEN REMOVAL(4,1)\|LAYER COMPACTION(4,1)\|MICROBIOLOGY(4,1)\|MINIMAL WASTE(4,1)\|MINING HAUL TRUCK NEED(4,1)\|MOLTEN CARBONATE FUEL CELL(4,1)\|MONITORING HEAT(4,1)\|NONHEATED BUFFER ZONE(4,1)\|NONOXIDIZING GAS(4,1)\|OIL BLEND(4,1)\|OPTIMIZATION REASON(4,1)\|PIPELINE EXTENSION(4,1)\|PLANT FIBER CELLULOSE(4,1)\|POLYMERIC RESIN(4,1)\|PRECAST PIECE(4,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(4,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(4,1)\|QUALITY DETERIORATION(4,1)\|RECOVERED HYDROCARBON LIQUID(4,1)\|RECOVERING OIL(4,1)\|REFORMATION(4,1)\|RESIDUAL HYDROCARBON PRODUCT(4,1)\|RESIDUAL SHALE REDUCED WETTING(4,1)\|RICH OIL BEARING ORE(4,1)\|ROTATING RETORT(4,1)\|SAND PARTICLE(4,1)\|SEQUENTIAL SOLUTION RECOVERY(4,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(4,1)\|SOLVENT SUBSTITUTED COMPOUND(4,1)\|STAGED PROCESSING(4,1)\|STEAM INJECTION(4,1)\|TECHNICAL CHALLENGE(4,1)\|TREMENDOUS VOLUME(4,1)\|UNCONTROLLED ESCAPE PREVENTION(4,1)\|UNCONTROLLED MIGRATION PREVENTION(4,1)\|VAPOROUS COMPONENT(4,1)\|VARIED ENZYME(4,1)\|VOLATILE ORGANIC(4,1)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOLEACHING(3,1)\|BIOMATERIAL(3,1)\|BIOOXIDATION(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ECONOMICS(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|EXCLUSION(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCLUSION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|LAYER CONDUIT(3,1)\|LAYING WIRE(3,1)\|LIGHTER(3,1)\|LIMITED COMBUSTION INTENT(3,1)\|LIQUID CONDENSATION(3,1)\|LIQUID EMULSION(3,1)\|LUBRICANT COOLANT(3,1)\|\|(IN1891/MUMNP/2011)\|HYDROCARBONACEOUS MATERIAL(100,44)\|INFRASTRUCTURE(100,22)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,13)\|CONSTRUCTED PERMEABILITY(100,12)\|RECOVERING HYDROCARBON(100,12)\|ENCAPSULATED VOLUME(88,24)\|GASEOUS FLUID(60,5)\|GASEOUS COMPONENT(54,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(51,6)\|FLUSH RESIDUAL HYDROCARBON(39,1)\|FLUSH HYDROCARBON VAPOR(38,1)\|COLLECTING REMOVED HYDROCARBON(37,1)\|CONTROL INFRASTRUCTURE(31,21)\|HYDROCARBON COMBUSTION(28,2)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|PERMEABILITY CONTROL IMPOUNDMENT(26,4)\|HYDROCARBONACEOUS MATERIAL FLUSHING(26,1)\|GASEOUS MATERIAL(22,3)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|VOID SPACE(20,5)\|MALFUNCTION(20,1)\|SECTIONED CAPSULE IMPOUNDMENT(19,2)\|STOICHIOMETRIC CONDITION(19,2)\|TOTAL VOLUME(18,2)\|COMPACTED FILL CEILING(17,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(17,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|HEATED HYDROCARBONACEOUS MATERIAL(15,1)\|QUARRY CAPSULE IMPOUNDMENT(15,1)\|UNCAPPED CAPSULE IMPOUNDMENT(15,1)\|UNDERGROUND RUBBLE CHIMNEY(15,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(14,1)\|NANOCARBON FULLERENE ADDITIVE(14,1)\|STRUCTURED IMPOUNDMENT CAPSULE(14,1)\|HYDROCARBON PRODUCTION(13,11)\|PROPANE(12,6)\|CONTAINMENT CAPSULE(12,2)\|NEARBY IMPOUNDMENT(12,2)\|TAILING BERM(12,2)\|UNRECOVERED HYDROCARBON(12,2)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|COAL(11,7)\|PEAT(11,4)\|ENGINEERED PERMEABILITY BARRIER(11,1)\|HYDROCARBON UNCONTROLLED EGRESS(11,1)\|UNDERGROUND MINED HYDROCARBON(11,1)\|BENTONITE CLAY(10,2)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|BENCH MINING ELEVATION(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|EXTERIOR CAPSULE IMPOUNDMENT(10,1)\|GARBAGE IMPOUNDMENT(10,1)\|GRAVITY ASSISTED DRAINAGE PIPE(10,1)\|GRAVITY DRAINAGE ASSISTANCE(10,1)\|INDISCRIMINATE DUMPING(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|MANIPULATED GRADE SHALE(10,1)\|MEDIAN SIZE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|UNTAPPED RESOURCE(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|HEAT PIPE(9,6)\|CONSTRUCTED SULFUR CAPSULE(9,2)\|IMPOUNDMENT HEIGHT(9,2)\|VOID VOLUME(8,4)\|GUIDELINE(8,3)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CORE DRILLING(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MINING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|LIQUID PRODUCT(7,10)\|CONVECTIVE HEATING(7,2)\|CRUSHED GLASS(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HEATED CONDUIT(7,2)\|HEATING(7,2)\|HORIZONTAL MINING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|BIO LEACHING(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|LEAN SHALE(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|HYDROGEN DONOR(6,6)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|FLOOR CONSTRUCTION(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|CARBONATE DECOMPOSITION(6,1)\|CO2 EMISSION(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|KEROGEN OIL(5,4)\|HEATED FLUID(5,3)\|PIPING(5,3)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|BLASTING(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|ANAEROBIC CONDITION(5,1)\|AQUEOUS SLURRY(5,1)\|BARRIER MANUFACTURE(5,1)\|CAPACITY INDICATOR(5,1)\|CAPSULE IMPOUNDMENT AREA(5,1)\|CATALYZING GAS(5,1)\|CEILING CAP(5,1)\|CLAY PIPE(5,1)\|CO2 PRODUCTION(5,1)\|COMMINUTED MASS(5,1)\|COMPOSITION ADMIXTURE(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|DECREASED VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLUID DRAINAGE(5,1)\|FLUSHING GAS(5,1)\|GAS COMBUSTION HEATER(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GEO MEMBRANE LAYER(5,1)\|GEO SYNTHETIC MEMBRANE(5,1)\|GEOLOGICAL LOCATION(5,1)\|HEATING CONDUIT PLACEMENT(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBON VAPOR(5,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|IMPOUNDMENT USEFUL LIFE(5,1)\|INORGANIC MATTER(5,1)\|KEROGEN REMOVAL(5,1)\|LAYER COMPACTION(5,1)\|MICROBIOLOGY(5,1)\|MINIMAL WASTE(5,1)\|MINING HAUL TRUCK NEED(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONOXIDIZING GAS(5,1)\|OIL BLEND(5,1)\|OPTIMIZATION REASON(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PRECAST PIECE(5,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(5,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(5,1)\|QUALITY DETERIORATION(5,1)\|RECOVERED HYDROCARBON LIQUID(5,1)\|RECOVERING OIL(5,1)\|REFORMATION(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RESIDUAL SHALE REDUCED WETTING(5,1)\|RICH OIL BEARING ORE(5,1)\|ROTATING RETORT(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|STAGED PROCESSING(5,1)\|STEAM INJECTION(5,1)\|TECHNICAL CHALLENGE(5,1)\|TREMENDOUS VOLUME(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNCONTROLLED MIGRATION PREVENTION(5,1)\|VAPOROUS COMPONENT(5,1)\|VARIED ENZYME(5,1)\|VOLATILE ORGANIC(5,1)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOMATERIAL(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ECONOMICS(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|LAYER CONDUIT(3,1)\|LAYING WIRE(3,1)\|LIGHTER(3,1)\|LIMITED COMBUSTION INTENT(3,1)\|LIQUID CONDENSATION(3,1)\|LIQUID EMULSION(3,1)\|LUBRICANT COOLANT(3,1)\|\|(CA2752133)\|HYDROCARBONACEOUS MATERIAL(100,45)\|INFRASTRUCTURE(100,22)\|INFRASTRUCTURE CONSTRUCTION(100,22)\|POSITIVE PRESSURE(100,13)\|CONSTRUCTED PERMEABILITY(100,12)\|RECOVERING HYDROCARBON(100,12)\|ENCAPSULATED VOLUME(87,25)\|GASEOUS FLUID(60,5)\|GASEOUS COMPONENT(54,2)\|COMMINUTED HYDROCARBONACEOUS MATERIAL(51,6)\|FLUSH RESIDUAL HYDROCARBON(39,1)\|FLUSH HYDROCARBON VAPOR(38,1)\|COLLECTING REMOVED HYDROCARBON(37,1)\|CONTROL INFRASTRUCTURE(31,21)\|HYDROCARBON COMBUSTION(28,2)\|RECOVERABLE HYDROCARBON REMAINING VOLUME(28,1)\|PERMEABILITY CONTROL IMPOUNDMENT(26,4)\|HYDROCARBONACEOUS MATERIAL FLUSHING(26,1)\|GASEOUS MATERIAL(22,3)\|CRUSHED HYDROCARBONACEOUS MATERIAL(21,1)\|VOID SPACE(20,5)\|MALFUNCTION(20,1)\|SECTIONED CAPSULE IMPOUNDMENT(19,2)\|STOICHIOMETRIC CONDITION(19,2)\|TOTAL VOLUME(18,2)\|COMPACTED FILL CEILING(17,3)\|ENGINEERED CAPSULE CONTAINMENT IMPOUNDMENT(17,1)\|IMPOUNDMENT CAPSULE CONTAINMENT(16,1)\|UNDERGROUND FRESHWATER AQUIFER(16,1)\|LIGNITE(15,4)\|HEATED HYDROCARBONACEOUS MATERIAL(15,1)\|QUARRY CAPSULE IMPOUNDMENT(15,1)\|UNCAPPED CAPSULE IMPOUNDMENT(15,1)\|UNDERGROUND RUBBLE CHIMNEY(15,1)\|HYDROCARBONACEOUS DEPOSIT EXCAVATION(14,1)\|NANOCARBON FULLERENE ADDITIVE(14,1)\|STRUCTURED IMPOUNDMENT CAPSULE(14,1)\|HYDROCARBON PRODUCTION(13,11)\|PROPANE(12,6)\|CONTAINMENT CAPSULE(12,2)\|NEARBY IMPOUNDMENT(12,2)\|TAILING BERM(12,2)\|UNRECOVERED HYDROCARBON(12,2)\|BENTONITE AMENDED SOIL(12,1)\|BITUMEN SIMULTANEOUS UPGRADING(12,1)\|COAL(11,7)\|PEAT(11,4)\|ENGINEERED PERMEABILITY BARRIER(11,1)\|HYDROCARBON UNCONTROLLED EGRESS(11,1)\|UNDERGROUND MINED HYDROCARBON(11,1)\|BENTONITE CLAY(10,2)\|CAPSULE SECTION(10,2)\|HYDROCARBON RICHNESS(10,2)\|BENCH MINING ELEVATION(10,1)\|BIOEXTRACTION SCENARIO(10,1)\|CHALLENGING ENDEAVOR(10,1)\|COLLECTIVE IMPOUNDMENT(10,1)\|EXTERIOR CAPSULE IMPOUNDMENT(10,1)\|GARBAGE IMPOUNDMENT(10,1)\|GRAVITY ASSISTED DRAINAGE PIPE(10,1)\|GRAVITY DRAINAGE ASSISTANCE(10,1)\|INDISCRIMINATE DUMPING(10,1)\|INFRASTRUCTURE SHUTDOWN(10,1)\|MANIPULATED GRADE SHALE(10,1)\|MEDIAN SIZE(10,1)\|SEWAGE IMPOUNDMENT(10,1)\|SUBDIVIDED IMPOUNDMENT(10,1)\|UNTAPPED RESOURCE(10,1)\|WATERPROOF QUALITY ENGINEERING(10,1)\|HEAT PIPE(9,6)\|CONSTRUCTED SULFUR CAPSULE(9,2)\|IMPOUNDMENT HEIGHT(9,2)\|VOID VOLUME(8,4)\|GUIDELINE(8,3)\|IMPERMEABLE FLOOR LAYER(8,3)\|UNDISTURBED GEOLOGICAL FORMATION(8,3)\|CORE DRILLING(8,2)\|CAPSULE SUBDIVISION(8,1)\|CEMENT FORTIFICATION(8,1)\|COMPACTED GEOGRID(8,1)\|CONSTRUCTED PERMEABILITY IMPOUNDMENT(8,1)\|DIRTY FINE PARTICULATE(8,1)\|ECONOMIC CONCERN(8,1)\|ECONOMIC VALUATION(8,1)\|EMPTY IMPOUNDMENT(8,1)\|ENGINEERED CARBON REINFORCEMENT GRID(8,1)\|GEOPOLITICAL CONCERN(8,1)\|GEOSYNTHETIC FABRICS(8,1)\|GOVERNMENT FLUID MIGRATION REGULATION(8,1)\|GRAVITY DRAINAGE CONTOUR(8,1)\|HEATING MINED RUBBLE(8,1)\|IMPOUNDMENT COLLECTION(8,1)\|INFRASTRUCTURE STABILIZATION(8,1)\|MINING QUARRY(8,1)\|NEARBY INFRASTRUCTURE(8,1)\|NONCIRCULAR CONDUIT(8,1)\|NONPERMEABLE INSULATION(8,1)\|PILED RUBBLE(8,1)\|PIT EXCAVATION(8,1)\|PREFORMED PIECE STACKING(8,1)\|RESISTANT PVC LINER(8,1)\|RETURNING DILUENT ELIMINATION(8,1)\|SPRAYABLE REFRACTORY(8,1)\|SPRAYED GROUTING(8,1)\|STEPPED DOWNSLOPE(8,1)\|TRILLION BARREL(8,1)\|UNCOVERED CAPSULE(8,1)\|UNDERGROUND AQUIFER CONTAMINATION(8,1)\|LIQUID PRODUCT(7,10)\|CONVECTIVE HEATING(7,2)\|CRUSHED GLASS(7,2)\|EXCAVATED HYDROCARBONACEOUS MATERIAL DEPOSIT(7,2)\|HEATED CONDUIT(7,2)\|HEATING(7,2)\|HORIZONTAL MINING(7,2)\|AB INITIO(7,1)\|ADDRESS METHANEDIONE(7,1)\|ALMOST INSTANTANEOUS INTRODUCTION(7,1)\|API MODIFIER(7,1)\|CANADIAN TAR SAND(7,1)\|COMPACTED SOIL(7,1)\|COMPUTER ASSISTED MINING(7,1)\|CONTAINMENT BOUNDARY(7,1)\|CONVEYER RETRACTION(7,1)\|CRANE SUSPENDED EXCAVATOR(7,1)\|CRUSHED ORE(7,1)\|DESTINATION CAPSULE(7,1)\|ECONOMIC OPPORTUNITY(7,1)\|EXCAVATED CAVITY(7,1)\|EXTRACTION IMPOUNDMENT(7,1)\|GEOTEXTILE BAG(7,1)\|GOVERNMENTAL REGULATION(7,1)\|HYDROCARBONACEOUS FORMATION EXCAVATED VOLUME(7,1)\|HYDROLOGY MEASURE(7,1)\|IMPERMEABLE BARRIER ZONE(7,1)\|IMPORTED SAND(7,1)\|IMPOUNDMENT FLOOR(7,1)\|IMPOUNDMENT OUTSIDE PERIMETER(7,1)\|INTRINSIC PYROLYSIS(7,1)\|LEAN SHALE(7,1)\|MICROORGANISM STRAIN(7,1)\|NATIVE BACTERIA(7,1)\|NATURAL DISTRIBUTED COMBUSTOR(7,1)\|ORE SOLVENT EXTRACTION(7,1)\|PILLAR MINING(7,1)\|PORTABLE COMBUSTOR(7,1)\|REFORMING CATALYST(7,1)\|REFORMING ZONE(7,1)\|REINFORCED CEMENT(7,1)\|SOIL AMENDMENT(7,1)\|STEEL FABRICATED RETORT(7,1)\|STOICHIOMETRIC COMBUSTION(7,1)\|SUPER DISPOSITION(7,1)\|TAR SAND BITUMEN TREATMENT(7,1)\|HYDROGEN DONOR(6,6)\|CONVECTION(6,3)\|FIBERGLASS(6,3)\|FREEZE WALL(6,3)\|FLOOR CONSTRUCTION(6,2)\|ACCEPTED PIPELINE STANDARD(6,1)\|ACID HALIDE(6,1)\|AQUATHERMAL REACTION(6,1)\|BARRIER INSULATION(6,1)\|CAP BARRIER ZONE(6,1)\|CARBONATE DECOMPOSITION(6,1)\|CO2 EMISSION(6,1)\|COMPLICATED MACHINERY(6,1)\|DAMAGING STRESS(6,1)\|EGRESS EXIT(6,1)\|ELECTRICAL RESISTIVE HEATER(6,1)\|EMBEDDED CONDUIT(6,1)\|ENHANCE COMPACTION(6,1)\|ENHANCING BITUMEN REMOVAL(6,1)\|EXPLICITLY RECITED LIMIT(6,1)\|FILL COMPACTION(6,1)\|FLOOR LEVELING(6,1)\|FLUSH HYDROCARBON(6,1)\|GASEOUS PRODUCT MINIMIZATION(6,1)\|GEOLOGICAL RESERVE ANALYSIS(6,1)\|GLOBAL WARMING CONCERN(6,1)\|IMPOUNDMENT DEPTH(6,1)\|IMPOUNDMENT REGION(6,1)\|ISOLATED CAPSULE(6,1)\|LEACHATE PRODUCTION(6,1)\|LIBERATED GASEOUS PRODUCT(6,1)\|LOCALIZED HOTSPOT ELIMINATION(6,1)\|MINERAL LINER(6,1)\|MINING ORE GRADE(6,1)\|MOISTURE MIGRATION(6,1)\|OFFSITE CONSTRUCTED INFRASTRUCTURE FORMATION(6,1)\|ORE MOISTURE CONTENT(6,1)\|PERMEABILITY PARTICLE(6,1)\|PIPE PERFORATION(6,1)\|PLENTIFUL LIGHT HYDROCARBON(6,1)\|POLYMERIC REFUSE(6,1)\|REFRACTORY CEMENT PIPE(6,1)\|RESIN ION EXCHANGE(6,1)\|REUSABLE PIPE(6,1)\|RICHNESS SENSOR(6,1)\|SOIL COMPACTION(6,1)\|SOY INSULATION(6,1)\|SPENT SHALE SOLID RINSING(6,1)\|STRATOGRAPHIC LOCATION(6,1)\|SUPPLEMENTAL FUEL(6,1)\|SWELLING BEHAVIOR(6,1)\|SYNTHETIC GEOGRID(6,1)\|SYNTHETIC NANO CARBON(6,1)\|TAR SAND DEPOSIT(6,1)\|TOXIC EFFLUENT(6,1)\|ULTRASONIC GENERATOR(6,1)\|UNDISTURBED SOIL(6,1)\|VOLATILE HYDROCARBON(6,1)\|WATERTIGHT CAP(6,1)\|KEROGEN OIL(5,4)\|HEATED FLUID(5,3)\|PIPING(5,3)\|REMOVING HYDROCARBON(5,3)\|VAPOR PRODUCTION(5,3)\|ACRE(5,2)\|ADJACENT IMPOUNDMENT(5,2)\|AGITATION(5,2)\|AIR EMISSION(5,2)\|ANCHOR MEMBER(5,2)\|BLASTING(5,2)\|CAPSULE WALL(5,2)\|CRUSHING(5,2)\|ENVIRONMENTAL STEWARDSHIP(5,2)\|EXPLOSION(5,2)\|GABION(5,2)\|GEOMEMBRANE(5,2)\|HAULING(5,2)\|HYDROCARBON FLUID(5,2)\|HYDROGEN CONTENT(5,2)\|INNER CAPSULE(5,2)\|INVESTIGATION(5,2)\|RECLAMATION(5,2)\|ANAEROBIC CONDITION(5,1)\|AQUEOUS SLURRY(5,1)\|BARRIER MANUFACTURE(5,1)\|CAPACITY INDICATOR(5,1)\|CAPSULE IMPOUNDMENT AREA(5,1)\|CATALYZING GAS(5,1)\|CEILING CAP(5,1)\|CLAY PIPE(5,1)\|CO2 PRODUCTION(5,1)\|COMMINUTED MASS(5,1)\|COMPOSITION ADMIXTURE(5,1)\|CONCRETE PANEL(5,1)\|CONDUCTIVE CEMENT(5,1)\|CONSTRUCTED CAPSULE CONTAINMENT VESSEL(5,1)\|CONSTRUCTED IMPOUNDMENT(5,1)\|DECREASED VISCOSITY(5,1)\|DISPERSION FLUID SENSOR(5,1)\|DUST PARTICLE(5,1)\|ECONOMICALLY VIABLE SOURCE(5,1)\|FAST RECOVERY(5,1)\|FINE COLLECTION(5,1)\|FLUID DRAINAGE(5,1)\|FLUSHING GAS(5,1)\|GAS COMBUSTION HEATER(5,1)\|GASEOUS HYDROCARBON PRODUCT(5,1)\|GEO MEMBRANE LAYER(5,1)\|GEO SYNTHETIC MEMBRANE(5,1)\|GEOLOGICAL LOCATION(5,1)\|HEATING CONDUIT PLACEMENT(5,1)\|HOTSPOT LOCALIZATION(5,1)\|HYDROCARBON VAPOR(5,1)\|HYDROCARBONACEOUS MATERIAL HYDROXYLATION(5,1)\|HYDRODESULFURIZATION(5,1)\|IMPOUNDMENT USEFUL LIFE(5,1)\|INORGANIC MATTER(5,1)\|KEROGEN REMOVAL(5,1)\|LAYER COMPACTION(5,1)\|MICROBIOLOGY(5,1)\|MINIMAL WASTE(5,1)\|MINING HAUL TRUCK NEED(5,1)\|MOLTEN CARBONATE FUEL CELL(5,1)\|MONITORING HEAT(5,1)\|NONHEATED BUFFER ZONE(5,1)\|NONOXIDIZING GAS(5,1)\|OIL BLEND(5,1)\|OPTIMIZATION REASON(5,1)\|PIPELINE EXTENSION(5,1)\|PLANT FIBER CELLULOSE(5,1)\|POLYMERIC RESIN(5,1)\|PRECAST PIECE(5,1)\|PRIMARY CONSTRUCTED CAPSULE CONTAINMENT(5,1)\|PRIMARY CONSTRUCTED INFRASTRUCTURE(5,1)\|QUALITY DETERIORATION(5,1)\|RECOVERED HYDROCARBON LIQUID(5,1)\|RECOVERING OIL(5,1)\|REFORMATION(5,1)\|RESIDUAL HYDROCARBON PRODUCT(5,1)\|RESIDUAL SHALE REDUCED WETTING(5,1)\|RICH OIL BEARING ORE(5,1)\|ROTATING RETORT(5,1)\|SAND PARTICLE(5,1)\|SEQUENTIAL SOLUTION RECOVERY(5,1)\|SOLID UNDISTURBED FORMATION PERMEABILITY(5,1)\|SOLVENT SUBSTITUTED COMPOUND(5,1)\|STAGED PROCESSING(5,1)\|STEAM INJECTION(5,1)\|TECHNICAL CHALLENGE(5,1)\|TREMENDOUS VOLUME(5,1)\|UNCONTROLLED ESCAPE PREVENTION(5,1)\|UNCONTROLLED MIGRATION PREVENTION(5,1)\|VAPOROUS COMPONENT(5,1)\|VARIED ENZYME(5,1)\|VOLATILE ORGANIC(5,1)\|HEATING RATE(4,3)\|INJECTION RATE(4,3)\|ADDED PERMEABILITY(3,1)\|ADJACENT INFRASTRUCTURE(3,1)\|ADJACENT NONHYDROCARBON(3,1)\|AGGLOMERATION(3,1)\|AGGREGATE PRODUCTION(3,1)\|ALKENE(3,1)\|ALLOY CONSTRUCTION(3,1)\|ASPHALTENE(3,1)\|AVAILABLE ADDRESSING(3,1)\|BAUXITE(3,1)\|BERM SUPPORT(3,1)\|BINDER(3,1)\|BIOCATALYST(3,1)\|BIOLEACHING(3,1)\|BIOMATERIAL(3,1)\|BIOOXIDATION(3,1)\|BIOREACTION(3,1)\|BIORECOVERY(3,1)\|BITUMEN SOURCE(3,1)\|CALCINED PETROLEUM COKE(3,1)\|CAPSULE IMPOUNDMENT TREATMENT AREA(3,1)\|CATALYTICALLY ACTIVE METAL(3,1)\|COMMINUTED HYDROCARBONACEOUS MATERIAL MASS(3,1)\|COMPOSITE WALL(3,1)\|COMPOUND SUBSTITUTION(3,1)\|CONDENSABILITY(3,1)\|CONDUIT PASS(3,1)\|CONDUIT WALL(3,1)\|CONSTRUCTED CAPSULE CONSTRUCTION(3,1)\|COOLING PIPE(3,1)\|CYCLOHEXANE(3,1)\|CYCLOPENTANE(3,1)\|DANGER REDUCTION(3,1)\|DIFFERING LAYER(3,1)\|DISCHARGE PIPE(3,1)\|DISPERSION RATE(3,1)\|DOWN CHUTE(3,1)\|DRAINPIPE(3,1)\|ECONOMICS(3,1)\|ELECTRICITY(3,1)\|ELECTROLYSIS(3,1)\|ELECTROPLATING(3,1)\|EMBANKMENT(3,1)\|ENCLOSED VOLUME(3,1)\|EXCAVATION AREA(3,1)\|FINAL HYDROCARBON PRODUCT(3,1)\|FINAL PRODUCT RECOVERY(3,1)\|FINE MESH(3,1)\|FLOTATION(3,1)\|FLUID COMMUNICATION(3,1)\|FLUID DELIVERY(3,1)\|FLUID EXTRACTION(3,1)\|FLUIDITY(3,1)\|FOUNDATION(3,1)\|FRACTURING(3,1)\|FREEDOM(3,1)\|GAS BARRIER(3,1)\|GAS COLLECTION OUTLET(3,1)\|GAS GATHERING(3,1)\|GAS INGRESS(3,1)\|GAS INJECTION(3,1)\|GAS MIGRATION(3,1)\|GUARANTEE(3,1)\|HAPPENING(3,1)\|HARVESTED HYDROCARBONACEOUS MATERIAL(3,1)\|HEATING OIL SHALE(3,1)\|HEATING SERVICE(3,1)\|HEAVY OIL RECYCLING(3,1)\|HOLDING TANK PROXIMITY(3,1)\|HOT GAS FILTERING(3,1)\|HYDROCARBON GAS(3,1)\|HYDROCARBON MATERIAL BIOREMEDIATION(3,1)\|HYDROGENATION(3,1)\|IMPERMEABILITY(3,1)\|IMPERMEABLE LAYER(3,1)\|IMPERMEABLE WALL(3,1)\|IMPERVIOUS LAYER(3,1)\|IMPOUNDMENT SIZE(3,1)\|IMPOUNDMENT WALL CONSTRUCTION(3,1)\|INCORPORATION(3,1)\|INDIGENOUS PLANT(3,1)\|INERT ENVIRONMENT(3,1)\|INORGANIC COMPONENT(3,1)\|INTEGRAL IMPOUNDMENT STRUCTURE(3,1)\|INTERRUPTION(3,1)\|LANGUAGE(3,1)\|LAYER CONDUIT(3,1)\|LAYING WIRE(3,1)\|LIGHTER(3,1)\|LIMITED COMBUSTION INTENT(3,1)\|LIQUID CONDENSATION(3,1)\|LIQUID EMULSION(3,1)\|	(US8349171)\|What is claimed is:\|1. A method of recovering hydrocarbons from hydrocarbonaceous materials, comprising:\| a) forming a constructed permeability control infrastructure which defines a substantially encapsulated volume;\| b) introducing a comminuted hydrocarbonaceous material into the control infrastructure to form a permeable body of hydrocarbonaceous material;\| c) maintaining within said encapsulated volume a positive pressure relative to the pressure outside of said control infrastructure;\| d) heating the hydrocarbonaceous material sufficient to remove hydrocarbons therefrom such that the hydrocarbonaceous material is substantially stationary during heating;\| e) flushing a gaseous fluid substantially free of oxygen throughout the permeable body in order to substantially remove hydrocarbons and other gaseous components from the permeable body, wherein heating of said hydrocarbonaceous materials has been terminated and said gaseous fluid is passed throughout the permeable body at a low temperature relative to the temperature at which said hydrocarbonaceous materials have been heated to provide a cooling effect on said hydrocarbonaceous materials and flush residual hydrocarbons and other gaseous materials from within said encapsulated volume; and\| f) collecting removed hydrocarbons and other gaseous components.\|2. The method of claim 1, wherein the hydrocarbonaceous material comprises oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof.\|3. The method of claim 1, wherein the hydrocarbonaceous material comprises oil shale.\|4. The method of claim 1, wherein the permeable body consists essentially of crushed hydrocarbonaceous material having an average size from about 6 inches to about 2 feet.\|5. The method of claim 1, wherein the permeable body has a void space from about 10% to about 50% a total volume of the permeable body.\|6. The method of claim 1, wherein the permeable body has a void space from about 30% to about 45% a total volume of the permeable body.\|7. The method of claim 1, wherein the positive pressure is maintained by means of a plurality of conduits at least some of which are embedded within the permeable body and wherein at least some of said conduits are configured to introduce said gaseous fluid at a predetermined temperature so as to cause heating or cooling of said hydrocarbonaceous material.\|8. The method of claim 1, wherein said heating has been terminated as a result of the release of unwanted hydrocarbons of other gaseous materials due to a malfunction.\|9. The method of claim 1, wherein said heating has been terminated as a result of the removal of effectively recoverable amounts of hydrocarbons from said hydrocarbonaceous materials and said flushing continues for a time sufficient to allow removal of remaining volumes of recoverable hydrocarbons and other gaseous materials and the cooling of said hydrocarbonaceous materials.\|10. The method of claim 1, wherein said gaseous fluid is a member selected from the group consisting of hydrogen, nitrogen, propane, carbon dioxide, hydrocarbons, and combinations thereof.\|11. The method of claim 1, wherein the positive pressure is from about 1.01 atm to about 10 atm.\|12. The method of claim 1, wherein the positive pressure is from about 1.1 atm to about 4 atm.\|13. The method of claim 1, wherein heating of the permeable body is accomplished by hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen.\|14. The method of claim 1, wherein the constructed permeability control infrastructure comprises clay, bentonite clay, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon, filled geotextile bags, polymeric resins, or combinations thereof.\|15. The method of claim 1, wherein the constructed permeability control infrastructure has a foundation structural floor support of earthen material or local surface topography as a floor.\|16. A constructed permeability control infrastructure, comprising:\| a) a permeability control impoundment defining a substantially encapsulated volume, said impoundment having a foundation structural floor support of earthen material or local surface topography as a floor; and\| b) a comminuted hydrocarbonaceous material within the encapsulated volume forming a substantially stationary permeable body of hydrocarbonaceous material, wherein the impoundment is adapted such that a positive pressure is maintained in said encapsulated volume relative to the pressure outside of said control infrastructure and prevents the introduction of air or other oxidizing gases from entering the impoundment.\|17. The constructed permeability control infrastructure of claim 16, wherein the constructed permeability control infrastructure comprises clay, bentonite clay, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon, filled geotextile bags, polymeric resins, or combinations thereof.	(US8349171)\|RELATED APPLICATION\|[0001] This application claims priority to U.S. Provisional Patent Application No. 61/152,146, filed Feb. 12, 2009, which is incorporated herein by reference.\|(US8349171)\|BACKGROUND\|[0002] Global and domestic demand for fossil fuels continues to rise despite price increases and other economic and geopolitical concerns. As such demand continues to rise, research and investigation into finding additional economically viable sources of fossil fuels correspondingly increases. Historically, many have recognized the vast quantities of energy stored in oil shale, coal and tar sand deposits, for example. However, these sources remain a difficult challenge in terms of economically competitive recovery. Canadian tar sands have shown that such efforts can be fruitful, although many challenges still remain, including environmental impact, product quality, production costs and process time, among others.\|[0003] Estimates of world-wide oil shale reserves range from two to almost seven trillion barrels of oil, depending on the estimating source. Regardless, these reserves represent a tremendous volume and remain a substantially untapped resource. A large number of companies and investigators continue to study and test methods of recovering oil from such reserves. In the oil shale industry, methods of extraction have included underground rubble chimneys created by explosions, in-situ methods such as In-Situ Conversion Process (ICP) method (Shell Oil), and heating within steel fabricated retorts. Other methods have included in-situ radio frequency methods (microwaves), and “modified” in-situ processes wherein underground mining, blasting and retorting have been combined to make rubble out of a formation to allow for better heat transfer and product removal.\|[0004] Among typical oil shale processes, all face tradeoffs in economics and environmental concerns. No current process alone satisfies economic, environmental and technical challenges. Moreover, global warming concerns give rise to additional measures to address carbon dioxide (CO2) emissions which are associated with such processes. Methods are needed that accomplish environmental stewardship, yet still provide high-volume cost-effective oil production.\|[0005] Below ground in-situ concepts emerged based on their ability to produce high volumes while avoiding the cost of mining. While the cost savings resulting from avoiding mining can be achieved, the in-situ method requires heating a formation for a longer period of time due to the extremely low thermal conductivity and high specific heat of solid oil shale. Perhaps the most significant challenge for any in-situ process is the uncertainty and long term potential of water contamination that can occur with underground freshwater aquifers. In the case of Shell's ICP method, a “freeze wall” is used as a barrier to keep separation between aquifers and an underground treatment area. Although this is possible, no long term analysis has proven for extended periods to guarantee the prevention of contamination. Without guarantees and with even fewer remedies should a freeze wall fail, other methods are desirable to address such environmental risks.\|[0006] For this and other reasons, the need remains for methods and systems which can provide improved recovery of hydrocarbons from suitable hydrocarbon-containing materials, which have acceptable economics and avoid the drawbacks mentioned above.\|SUMMARY\|[0007] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating the hydrocarbonaceous material can be substantially stationary. Removed fluid hydrocarbons can be collected for further processing, use in the process as supplemental fuel or additives, and/or direct use without further treatment.\|[0008] These systems and processes can allow difficult problems to be solved related to the extraction of hydrocarbon liquids and gases from surface or underground mined hydrocarbon bearing deposits such as oil shale, tar sands, lignite, and coal, and from harvested biomass. Among other things, this approach helps reduce cost, increase volume output, lower air emissions, limit water consumption, prevent underground aquifer contamination, reclaim surface disturbances, reduce material handling costs, remove dirty fine particulates, and improve composition of recovered hydrocarbon liquid or gas. It also addresses water contamination issues with a safer, more predictable, engineered, observable, repairable, adaptable and preventable water protection structure.\|[0009] Additional features and advantages of the invention will be apparent from the following detailed description, which illustrates, by way of example, features of the invention.\|(US8349171)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0010] FIG. 1 is side partial cutaway view schematic of a constructed permeability control infrastructure in accordance with one embodiment.\|[0011] FIGS. 2A and 2B are top and plan views of a plurality of permeability control impoundments in accordance with one embodiment.\|[0012] FIG. 3 is a side cutaway view of a permeability control impoundment in accordance with one embodiment.\|[0013] FIG. 4 is a schematic of a portion of a constructed infrastructure in accordance with an embodiment.\|[0014] FIG. 5 is a schematic showing heat transfer between two permeability control impoundments in accordance with another embodiment.\|(US8349171)\|DETAILED DESCRIPTION\|[0015] It should be noted that the figures are merely exemplary of several embodiments and no limitations on the scope of the present invention are intended thereby. Further, the figures are generally not drawn to scale, but are drafted for purposes of convenience and clarity in illustrating various aspects of the invention.\|DETAILED DESCRIPTION\|[0016] Reference will now be made to exemplary embodiments and specific language will be used herein to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended. Alterations and further modifications of the inventive features described herein, and additional applications of the principles of the invention as described herein, which would occur to one skilled in the relevant art and having possession of this disclosure, are to be considered within the scope of the invention. Further, before particular embodiments are disclosed and described, it is to be understood that this invention is not limited to the particular process and materials disclosed herein as such may vary to some degree. It is also to be understood that the terminology used herein is used for the purpose of describing particular embodiments only and is not intended to be limiting, as the scope of the present invention will be defined only by the appended claims and equivalents thereof.\|DEFINITIONS\|[0017] In describing and claiming the present invention, the following terminology will be used.\|[0018] The singular forms “a,” “an,” and “the” include plural references unless the context clearly dictates otherwise. Thus, for example, reference to “a wall” includes reference to one or more of such structures, “a permeable body” includes reference to one or more of such materials, and “a heating step” refers to one or more of such steps.\|[0019] As used herein “existing grade” or similar terminology refers to the grade or a plane parallel to the local surface topography of a site containing an infrastructure as described herein which infrastructure may be above or below the existing grade.\|[0020] As used herein, “conduits” refers to any passageway along a specified distance which can be used to transport materials and/or heat from one point to another point. Although conduits can generally be circular pipes, other non-circular conduits can also be useful. Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|[0021] As used herein, “constructed infrastructure” refers to a structure which is substantially entirely man made, as opposed to freeze walls, sulfur walls, or other barriers which are formed by modification or filling pores of an existing geological formation.\|[0022] The constructed permeability control infrastructure is often substantially free of undisturbed geological formations, although the infrastructure can be formed adjacent or in direct contact with an undisturbed formation. Such a control infrastructure can be unattached or affixed to an undisturbed formation by mechanical means, chemical means or a combination of such means, e.g. bolted into the formation using anchors, ties, or other suitable hardware.\|[0023] As used herein, “comminuted” refers to breaking a formation or larger mass into pieces. A comminuted mass can be rubbilized or otherwise broken into fragments.\|[0024] As used herein, “hydrocarbonaceous material” refers to any hydrocarbon-containing material from which hydrocarbon products can be extracted or derived. For example, hydrocarbons may be extracted directly as a liquid, removed via solvent extraction, directly vaporized or otherwise removed from the material. However, many hydrocarbonaceous materials contain kerogen or bitumen which is converted to a hydrocarbon through heating and pyrolysis. Hydrocarbonaceous materials can include, but is not limited to, oil shale, tar sands, coal, lignite, bitumen, peat, and other organic materials.\|[0025] As used herein, “impoundment” refers to a structure designed to hold or retain an accumulation of fluid and/or solid moveable materials. An impoundment generally derives at least a substantial portion of foundation and structural support from earthen materials. Thus, the control walls do not always have independent strength or structural integrity apart from the earthen material and/or formation against which they are formed.\|[0026] As used herein, “permeable body” refers to any mass of comminuted hydrocarbonaceous material having a relatively high permeability which exceeds permeability of a solid undisturbed formation of the same composition. Suitable permeable bodies can have greater than about 10% void space and typically have void space from about 30% to 45%, although other ranges may be suitable. Allowing for high permeability facilitates, for example, through the incorporation of large irregularly shaped particles, heating of the body through convection as the primary heat transfer while also substantially reducing costs associated with crushing to very small sizes, e.g. below about 1 to about 0.5 inch.\|[0027] As used herein, “wall” refers to any constructed feature having a permeability control contribution to confining material within an encapsulated volume defined at least in part by control walls. Walls can be oriented in any manner such as vertical, although ceilings, floors and other contours defining the encapsulated volume can also be “walls” as used herein.\|[0028] As used herein, “mined” refers to a material which has been removed or disturbed from an original stratographic or geological location to a second and different location or returned to the same location. Typically, mined material can be produced by rubbilizing, crushing, explosively detonating, or otherwise removing material from a geologic formation.\|[0029] As used herein, “substantially stationary” refers to nearly stationary positioning of materials with a degree of allowance for subsidence, expansion, and/or settling as hydrocarbons are removed from the hydrocarbonaceous material from within the enclosed volume to leave behind lean material. In contrast, any circulation and/or flow of hydrocarbonaceous material such as that found in fluidized beds or rotating retorts involves highly substantial movement and handling of hydro carbonaceous material.\|[0030] As used herein, “substantial” when used in reference to a quantity or amount of a material, or a specific characteristic thereof, refers to an amount that is sufficient to provide an effect that the material or characteristic was intended to provide. The exact degree of deviation allowable may in some cases depend on the specific context. Similarly, “substantially free of” or the like refers to the lack of an identified element or agent in a composition. Particularly, elements that are identified as being “substantially free of” are either completely absent from the composition, or are included only in amounts which are small enough so as to have no measurable effect on the composition.\|[0031] As used herein, “about” refers to a degree of deviation based on experimental error typical for the particular property identified. The latitude provided the term “about” will depend on the specific context and particular property and can be readily discerned by those skilled in the art. The term “about” is not intended to either expand or limit the degree of equivalents which may otherwise be afforded a particular value. Further, unless otherwise stated, the term “about” shall expressly include “exactly,” consistent with the discussion below regarding ranges and numerical data.\|[0032] Concentrations, dimensions, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of about 1 to about 200 should be interpreted to include not only the explicitly recited limits of 1 and 200, but also to include individual sizes such as 2, 3, 4, and sub-ranges such as 10 to 50, 20 to 100, etc.\|[0033] As used herein, a plurality of items, structural elements, compositional elements, and/or materials may be presented in a common list for convenience. However, these lists should be construed as though each member of the list is individually identified as a separate and unique member. Thus, no individual member of such list should be construed as a de facto equivalent of any other member of the same list solely based on their presentation in a common group without indications to the contrary.\|[0034] Recovering Hydrocarbons from Hydrocarbonaceous Materials Under Positive Pressure\|[0035] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined or harvested hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure is a fixed structure. Removed fluid hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.\|[0036] The constructed permeability control infrastructure can be formed using existing grade as floor support and/or as side wall support for the constructed infrastructure. For example, the control infrastructure can be formed as a free standing structure, i.e. using only existing grade as a floor with side walls being man-made. Alternatively, the control infrastructure can be formed within an excavated pit.\|[0037] A constructed permeability control infrastructure can include a permeability control impoundment which defines a substantially encapsulated volume. The permeability control impoundment is substantially free of undisturbed geological formations. Specifically, the permeability control aspect of the impoundment can be completely constructed and manmade as a separate isolation mechanism for prevention of uncontrolled migration of material into or out of the encapsulated volume.\|[0038] In one embodiment, the permeability control impoundment can be formed along walls of an excavated hydrocarbonaceous material deposit. For example, oil shale, tar sands, or coal can be mined from a deposit to form a cavity which corresponds approximately to a desired encapsulation volume for an impoundment. The excavated cavity can then be used as a form and support to create the permeability control impoundment.\|[0039] In one alternative aspect, at least one additional excavated hydrocarbonaceous material deposit can be formed such that a plurality of impoundments can be operated. Further, such a configuration can facilitate a reduction in transportation distance of the mined material. Specifically, the mined hydrocarbonaceous material for any particular encapsulated volume can be mined from an adjacent excavated hydrocarbonaceous material deposit. In this manner, a grid of constructed structures can be built such that mined material can be immediately and directly filled into an adjacent impoundment.\|[0040] Mining and/or excavation of hydro carbonaceous deposits can be accomplished using any suitable technique. Conventional surface mining can be used, although alternative excavators can also be used without requirement of transportation of the mined materials. In one specific embodiment, the hydrocarbonaceous deposit can be excavated using a crane-suspended excavator. One example of a suitable excavator can include vertical tunnel boring machines. Such machines can be configured to excavate rock and material beneath the excavator. As material is removed, the excavator is lowered to ensure substantially continuous contact with a formation. Removed material can be conveyed out of the excavation area using conveyors or lifts. Alternatively, the excavation can occur under aqueous slurry conditions to reduce dust problems and act as a lubricant/coolant. The slurry material can be pumped out of the excavation for separation of solids in a settling tank or other similar solid-liquid separator, or the solids may be allowed to precipitate directly in an impoundment. This approach can be readily integrated with simultaneous or sequential solution-based recovery of metals and other materials as described in more detail below.\|[0041] Further, excavation and formation of a permeability control impoundment can be accomplished simultaneously. For example, an excavator can be configured to remove hydro carbonaceous material while side walls of an impoundment are formed. Material can be removed from just underneath edges of the side walls such that the walls can be guided downward to allow additional wall segments to be stacked above. This approach can allow for increased depths while avoiding or reducing dangers of cave-in prior to formation of supporting impoundment walls.\|[0042] The impoundment can be formed of any suitable material which provides isolation of material transfer across walls of the impoundment. In this manner, integrity of the walls is retained during operation of the control infrastructure sufficient to substantially prevent uncontrolled migration of fluids outside of the control infrastructure. Non-limiting examples of suitable material for use in forming the impoundment of the constructed permeability control infrastructure can include clay, bentonite clay (e.g. clay comprising at least a portion of bentonite), bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, or combinations thereof. Engineered cementitious composites (ECC) materials, fiber reinforced composites, and the like can be particularly strong and can be readily engineered to meet permeability and temperature tolerance requirements of a given installation. As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required. For example, materials having a melting point above the maximum operating temperature of the infrastructure can be useful to maintain containment during and after heating and recovery. However, lower temperature materials can also be used if a non-heated buffer zone is maintained between the walls and heated portions of the permeable body. Such buffer zones can range from 6 inches to 50 feet depending on the particular material used for the impoundment and the composition of the permeable body. In another aspect, walls of the impoundment can be acid, water and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water. For impoundment walls formed along formations or other solid support, the impoundment walls can be formed of a sprayed grouting, sprayed liquid emulsions, or other sprayed material such as sprayable refractory grade grouting which forms a seal against the formation and creates the permeability control wall of the impoundments. Impoundment walls may be substantially continuous such that the impoundment defines the encapsulated volume sufficiently to prevent substantial movement of fluids into or out of the impoundment other than defined inlets and outlets, e.g. via conduits or the like as discussed herein. In this manner, the impoundments can readily meet government fluid migration regulations. Alternatively, or in combination with a manufactured barrier, portions of the impoundment walls can be undisturbed geological formation and/or compacted earth. In such cases, the constructed permeability control infrastructure is a combination of permeable and impermeable walls as described in more detail below.\|[0043] In one detailed aspect, a portion of hydrocarbonaceous material, either pre- or post-processed, can be used as a cement fortification and/or cement base which are then poured in place to form portions or the entirety of walls of the control infrastructure. These materials can be formed in place or can be preformed and then assembled on site to form an integral impoundment structure. For example, the impoundment can be constructed by cast forming in place as a monolithic body, extrusion, stacking of preformed or precast pieces, concrete panels joined by a grout (cement, ECC or other suitable material), inflated form, or the like. The forms can be built up against a formation or can be stand alone structures. Forms can be constructed of any suitable material such as, but not limited to, steel, wood, fiberglass, polymer, or the like. The forms can be assembled in place or may be oriented using a crane or other suitable mechanism. Alternatively, the constructed permeability control infrastructure can be formed of gabions and/or geosynthetic fabrics assembled in layers with compacted fill material. Optional binders can be added to enhance compaction of the permeability control walls. In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|[0044] Impoundment walls can optionally include non-permeable insulation and/or fines collection layers. These permeable layers can be oriented between the permeability control barrier and the permeable body. For example, a layer of hydrocarbonaceous comminuted material can be provided which allows fluids to enter, cool, and at least partially condense within the layer. Such permeable layer material can generally have a particle size smaller than the permeable body. Further, such hydrocarbonaceous material can remove fines from passing fluids via various attractive forces. In one embodiment, the construction of impoundment walls and floors can include multiple compacted layers of indigenous or manipulated low grade shale with any combination of sand, cement, fiber, plant fiber, nano carbons, crushed glass, reinforcement steel, engineered carbon reinforcement grid, calcium salts, and the like. In addition to such composite walls, designs which inhibit long term fluid and gas migration through additional impermeability engineering can be employed including, but not limited to, liners, geo-membranes, compacted soils, imported sand, gravel or rock and gravity drainage contours to move fluids and gases away from impervious layers to egress exits. Impoundment floor and wall construction, can, but need not comprise, a stepped up or stepped down slope or bench as the case of mining course may dictate following the optimal ore grade mining. In any such stepped up or down applications, floor leveling and containment wall construction can typically drain or slope to one side or to a specific central gathering area(s) for removal of fluids by gravity drainage assistance.\|[0045] Optionally, capsule wall and floor construction can include insulation which prevents heat transfer outside of the constructed infrastructure or outside of inner capsules or conduits within the primary constructed capsule containment. Insulation can comprise manufactured materials, cement or various materials other materials which are less thermally conductive than surrounding masses, i.e. permeable body, formation, adjacent infrastructures, etc. Thermally insulating barriers can also be formed within the permeable body, along impoundment walls, ceilings and/or floors. One detailed aspect includes the use of biodegradable insulating materials, e.g. soy insulation and the like. This is consistent with embodiments wherein the impoundment is a single use system such that insulations, pipes, and/or other components can have a relatively low useful life, e.g. less than 1-2 years. This can reduce equipment costs as well as reduce long-term environmental impact.\|[0046] These structures and methods can be applied at almost any scale. Larger encapsulated volumes and increased numbers of impoundments can readily produce hydrocarbon products and performance comparable to or exceeding smaller constructed infrastructures. As an illustration, single impoundments can range in size from tens of meters across to tens of acres. Optimal impoundment sizes may vary depending on the hydrocarbonaceous material and operating parameters, however it is expected that suitable areas can range from about one-half to five acres in top plan surface area.\|[0047] The methods and infrastructures can be used for recovery of hydrocarbons from a variety of hydrocarbonaceous materials. One particular advantage is a wide degree of latitude in controlling particle size, conditions, and composition of the permeable body introduced into the encapsulated volume. Non-limiting examples of mined hydrocarbonaceous material which can be treated comprise oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof. In some cases it can be desirable to provide a single type of hydrocarbonaceous material so that the permeable body consists essentially of one of the above materials. However, the permeable body can include mixtures of these materials such that grade, oil content, hydrogen content, permeability and the like can be adjusted to achieve a desired result. Further, different hydrocarbon materials can be placed in multiple layers or in a mixed fashion such as combining coal, oil shale, tar sands, biomass, and/or peat.\|[0048] In one embodiment, hydrocarbon containing material can be classified into various inner capsules within a primary constructed infrastructure for optimization reasons. For instance, layers and depths of mined oil shale formations may be richer in certain depth pay zones as they are mined. Once, blasted, mined, shoveled and hauled inside of capsule for placement, richer oil bearing ores can be classified or mixed by richness for optimal yields, faster recovery, or for optimal averaging within each impoundment. Further, providing layers of differing composition can have added benefits. For example, a lower layer of tar sands can be oriented below an upper layer of oil shale. Generally, the upper and lower layers can be in direct contact with one another although this is not required. The upper layer can include heating pipes embedded therein as described in more detail below. The heating pipes can heat the oil shale sufficient to liberate kerogen oil, including short-chain liquid hydrocarbons, which can act as a solvent for bitumen removal from the tar sands. In this manner, the upper layer acts as an in situ solvent source for enhancing bitumen removal from the lower layer. Heating pipes within the lower layer are optional such that the lower layer can be free of heating pipes or may include heating pipes, depending on the amount of heat transferred via downward passing liquids from the upper layer and any other heat sources. The ability to selectively control the characteristics and composition of the permeable body adds a significant amount of freedom in optimizing oil yields and quality.\|[0049] Furthermore, in many embodiments, the liberated gaseous and liquid products act as an in situ produced solvent which supplements kerogen removal and/or additional hydrocarbon removal from the hydro carbonaceous material.\|[0050] In yet another detailed aspect, the permeable body can further comprise an additive or biomass. Additives can include any composition which acts to increase the quality of removed hydrocarbons, e.g. increased API, decreased viscosity, improved flow properties, reduced wetting of residual shale, reduction of sulfur, hydrogenation agents, etc. Non-limiting examples of suitable additives can include bitumen, kerogen, propane, natural gas, natural gas condensate, crude oil, refining bottoms, asphaltenes, common solvents, other diluents, and combinations of these materials. In one specific embodiment, the additive can include a flow improvement agent and/or a hydrogen donor agent. Some materials can act as both or either agents to improve flow or as a hydrogen donor. Non-limiting examples of such additives can include methane, natural gas condensates, common solvent such as acetone, toluene, benzene, etc., and other additives listed above. Additives can act to increase the hydrogen to carbon ratio in any hydrocarbon products, as well as act as a flow enhancement agent. For example, various solvents and other additives can create a physical mixture which has a reduced viscosity and/or reduced affinity for particulate solids, rock and the like. Further, some additives can chemically react with hydrocarbons and/or allow liquid flow of the hydrocarbon products. Any additives used can become part of a final recovered product or can be removed and reused or otherwise disposed of.\|[0051] Similarly, biological hydroxylation of hydrocarbonaceous materials to form synthetic gas or other lighter weight products can be accomplished using known additives and approaches. Enzymes or biocatalysts can also be used in a similar manner. Further, manmade materials can also be used as additives such as, but not limited to, tires, polymeric refuse, or other hydrocarbon-containing materials.\|[0052] Although these methods are broadly applicable, as a general guideline, the permeable body can include particles from about ⅛ inch to about 6 feet in largest dimension, and in some cases less than 1 foot and in other cases less than about 6 inches. However, as a practical matter, sizes from about 2 inches to about 2 feet can provide good results with about 1 foot diameter being useful for oil shale especially. Void space can be an important factor in determining optimal particle diameters. As a general matter, any functional void space can be used; however, about 10% to about 50% and in some cases about 30% to about 45% usually provides a good balance of permeability and effective use of available volumes. Void volumes can be varied somewhat by varying other parameters such as heating conduit placement, additives, and the like. Mechanical separation of mined hydrocarbonaceous materials allows creation of fine mesh, high permeability particles which enhance thermal dispersion rates once placed in capsule within the impoundment. The added permeability allows for more reasonable, low temperatures which also help to avoid higher temperatures which result in greater CO2 production from carbonate decomposition and associated release of trace heavy metals, volatile organics, and other compounds which can create toxic effluent and/or undesirable materials which can be monitored and controlled.\|[0053] In one embodiment, computer assisted mining, mine planning, hauling, blasting, assay, loading, transport, placement, and dust control measures can be utilized to fill and optimize the speed of mined material movement into the constructed capsule containment structure. In one alternative aspect, the impoundments can be formed in excavated volumes of a hydrocarbonaceous formation, although other locations remote from the control infrastructure can also be useful. For example, some hydrocarbonaceous formations have relatively thin hydrocarbon-rich layers, e.g. less than about 300 feet thick. Therefore, vertical mining and drilling tend to not be cost effective. In such cases, horizontal mining can be useful to recover the hydrocarbonaceous materials for formation of the permeable body. Although horizontal mining continues to be a challenging endeavor, a number of technologies have been developed and continue to be developed which can be useful in connection with the impoundments. In such cases, at least a portion of the impoundment can be formed across a horizontal layer, while other portions of the impoundment can be formed along and/or adjacent non-hydrocarbon bearing formation layers. Other mining approaches such as, but not limited to, room and pillar mining can provide an effective source of hydrocarbonaceous material with minimal waste and/or reclamation which can be transported to an impoundment and treated in accordance with these principles.\|[0054] As mentioned herein, these systems and processes allow for a large degree of control regarding properties and characteristics of the permeable body which can be designed and optimized for a given installation. Impoundments, individually and across a plurality of impoundments can be readily tailored and classified based on varying composition of materials, intended products and the like. For example, several impoundments can be dedicated to production of heavy crude oil, while others can be configured for production of lighter products and/or syn gas. Non-limiting example of potential classifications and factors can include catalyst activity, enzymatic reaction for specific products, aromatic compounds, hydrogen content, microorganism strain or purpose, upgrading process, target final product, pressure (effects product quality and type), temperature, swelling behavior, aquathermal reactions, hydrogen donor agents, heat superdisposition, garbage impoundment, sewage impoundment, reusable pipes, and others. Typically, a plurality of these factors can be used to configure impoundments in a given project area for distinct products and purposes.\|[0055] The comminuted hydrocarbonaceous material can be filled into the control infrastructure to form the permeable body in any suitable manner. Typically the comminuted hydrocarbonaceous material can be conveyed into the control infrastructure by dumping, conveyors or other suitable approaches. As mentioned previously, the permeable body can have a suitably high void volume. Indiscriminate dumping can result in excessive compaction and reduction of void volumes. Thus, the permeable body can be formed by low compaction conveying of the hydrocarbonaceous material into the infrastructure. For example, retracting conveyors can be used to deliver the material near a top surface of the permeable body as it is formed. In this way, the hydrocarbonaceous material can retain a significant void volume between particles without substantial further crushing or compaction despite some small degree of compaction which often results from lithostatic pressure as the permeable body is formed.\|[0056] Once a desired permeable body has been formed within the control infrastructure, heat can be introduced sufficient to begin removal of hydrocarbons, e.g. via pyrolysis. A suitable heat source can be thermally associated with the permeable body. Optimal operating temperatures within the permeable body can vary depending on the composition and desired products. However, as a general guideline, operating temperatures can range from about 200° F. to about 750° F. Temperature variations throughout the encapsulated volume can vary and may reach as high as 900° F. or more in some areas. In one embodiment, the operating temperature can be a relatively lower temperature to facilitate production of liquid product such as from about 200° F. to about 650° F. This heating step can be a roasting operation which results in beneficiation of the crushed ore of the permeable body. Further, one embodiment comprises controlling the temperature, pressure and other variables sufficient to produce predominantly, and in some cases substantially only, liquid product. Generally, products can include both liquid and gaseous products, while liquid products can require fewer processing steps such as scrubbers etc. The relatively high permeability of the permeable body allows for production of liquid hydrocarbon products and minimization of gaseous products, depending to some extent on the particular starting materials and operating conditions. In one embodiment, the recovery of hydrocarbon products can occur substantially in the absence of cracking within the permeable body.\|[0057] In one aspect, heat can be transferred to the permeable body via convection. Heated gases can be injected into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body. Heated gases can be produced by combustion of natural gas, hydrocarbon product, or any other suitable source. The heated gases can be imported from external sources or recovered from the process.\|[0058] Alternatively, or in combination with convective heating, a highly configurable approach can include embedding a plurality of conduits within the permeable body. The conduits can be configured for use as heating pipes, cooling pipes, heat transfer pipes, drainage pipes, or gas pipes. Further, the conduits can be dedicated to a single function or may serve multiple functions during operation of the infrastructure, i.e. heat transfer and drainage. The conduits can be formed of any suitable material, depending on the intended function. Non-limiting examples of suitable materials can include clay pipes, refractory cement pipes, refractory ECC pipes, poured in place pipes, metal pipes such as cast iron, stainless steel etc., polymer such as PVC, and the like. In one specific embodiment, all or at least a portion of the embedded conduits can comprise a degradable material. For example, non-galvanized 6″ cast iron pipes can be effectively used for single use embodiments and perform well over the useful life of the impoundment, typically less than about 2 years. Further, different portions of the plurality of conduits can be formed of different materials. Poured in place pipes can be especially useful for very large encapsulation volumes where pipe diameters exceed several feet. Such pipes can be formed using flexible wraps which retain a viscous fluid in an annular shape. For example, PVC pipes can be used as a portion of a form along with flexible wraps, where concrete or other viscous fluid is pumped into an annular space between the PVC and flexible wrap. Depending on the intended function, perforations or other apertures can be made in the conduits to allow fluids to flow between the conduits and the permeable body. Typical operating temperatures exceed the melting point of conventional polymer and resin pipes. In some embodiments, the conduits can be placed and oriented such that the conduits intentionally melt or otherwise degrade during operation of the infrastructure.\|[0059] The plurality of conduits can be readily oriented in any configuration, whether substantially horizontal, vertical, slanted, branched, or the like. At least a portion of the conduits can be oriented along predetermined pathways prior to embedding the conduits within the permeable body. The predetermined pathways can be designed to improve heat transfer, gas-liquid-solid contacting, maximize fluid delivery or removal from specific regions within the encapsulated volume, or the like. Further, at least a portion the conduits can be dedicated to heating of the permeable body. These heating conduits can be selectively perforated to allow heated gases or other fluids to convectively heat and mix throughout the permeable body. The perforations can be located and sized to optimize even and/or controlled heating throughout the permeable body. Alternatively, the heating conduits can form a closed loop such that heating gases or fluids are segregated from the permeable body. Thus, a “closed loop” does not necessarily require recirculation, rather isolation of heating fluid from the permeable body. In this manner, heating can be accomplished primarily or substantially only through thermal conduction across the conduit walls from the heating fluids into the permeable body. Heating in a closed loop allows for prevention of mass transfer between the heating fluid and permeable body and can reduce formation and/or extraction of gaseous hydrocarbon products.\|[0060] During the heating or roasting of the permeable body, localized areas of heat which exceed parent rock decomposition temperatures, often above about 900° F., can reduce yields and form carbon dioxide and undesirable contaminating compounds which can lead to leachates containing heavy metals, soluble organics and the like. The heating conduits can allow for substantial elimination of such localized hot spots while maintaining a vast majority of the permeable body within a desired temperature range. The degree of uniformity in temperature can be a balance of cost (e.g. for additional heating conduits) versus yields. However, at least about 85% of the permeable body can readily be maintained within about 5-10% of a target temperature range with substantially no hot spots, i.e. exceeding the decomposition temperature of the hydrocarbonaceous materials such as about 800° F. and in many cases about 900° F. Thus, operated as described herein, the systems can allow for recovery of hydrocarbons while eliminating or substantially avoiding production of undesirable leachates. Although products can vary considerably depending on the starting materials, high quality liquid and gaseous products are possible. In accordance with one embodiment, a crushed oil shale material can produce a liquid product having an API from about 30 to about 45, with about 33 to about 38 being currently typical, directly from the oil shale without additional treatment. Interestingly, practice of these principles has led to an understanding that pressure appears to be a much less influential factor on the quality of recovered hydrocarbons than temperature and heating times. Although heating times can vary considerably, depending on void space, permeable body composition, quality, etc., as a general guideline times can range from a few days (i.e. 3-4 days) up to about one year. In one specific example, heating times can range from about 2 weeks to about 4 months. Under-heating oil shale at short residence times, i.e. minutes to several hours, can lead to formation of leachable and/or somewhat volatile hydrocarbons. Accordingly, these systems and processes allow for extended residence times at moderate temperatures such that organics present in oil shale can be volatilized and/or carbonized, leaving insubstantial leachable organics. In addition, the underlying shale is not generally decomposed or altered which reduces soluble salt formation.\|[0061] Further, conduits can be oriented among a plurality of impoundments and/or control infrastructures to transfer fluids and/or heat between the structures. The conduits can be welded to one another using conventional welding or the like. Further, the conduits can include junctions which allow for rotation and or small amounts of movement during expansion and subsidence of material in the permeable body. Additionally, the conduits can include a support system which acts to support the assembly of conduits prior to and during filling of the encapsulated volume, as well as during operation. For example, during heating flows of fluids, heating and the like can cause expansion (fracturing or popcorn effect) or subsidence sufficient to create potentially damaging stress and strain on the conduits and associated junctions. A truss support system or other similar anchoring members can be useful in reducing damage to the conduits. The anchoring members can include cement blocks, 1-beams, rebar, columns, etc. which can be associated with walls of the impoundment, including side walls, floors and ceilings.\|[0062] Alternatively, the conduits can be completely constructed and assembled prior to introduction of any mined materials into the encapsulated volume. Care and planning can be considered in designing the predetermined pathways of the conduits and method of filling the volume in order to prevent damage to the conduits during the filling process as the conduits are buried. Thus, as a general rule, the conduits used are oriented ab initio, or prior to embedding in the permeable body such that they are non-drilled. As a result, construction of the conduits and placement thereof can be performed without extensive core drilling and/or complicated machinery associated with well-bore or horizontal drilling. Rather, horizontal or any other orientation of conduit can be readily achieved by assembling the desired predetermined pathways prior to, or contemporaneous with, filling the infrastructure with the mined hydrocarbonaceous material. The non-drilled, hand/crane-placed conduits oriented in various geometric patterns can be laid with valve controlled connecting points which yield precise and closely monitored heating within the capsule impoundment. The ability to place and layer conduits including connecting, bypass and flow valves, and direct injection and exit points, allow for precision temperature and heating rates, precision pressure and pressurization rates, and precision fluid and gas ingress, egress and composition admixtures. For example, when a bacteria, enzyme, or other biological material is used, optimal temperatures can be readily maintained throughout the permeable body to increase performance, reaction, and reliability of such biomaterials.\|[0063] The conduits will generally pass through walls of the constructed infrastructure at various points. Due to temperature differences and tolerances, it can be beneficial to include an insulating material at the interface between the wall and the conduits. The dimensions of this interface can be minimized while also allowing space for thermal expansion differences during startup, steady-state operation, fluctuating operating conditions, and shutdown of the infrastructure. The interface can also involve insulating materials and sealant devices which prevent uncontrolled egress of hydrocarbons or other materials from the control infrastructure. Non-limiting examples of suitable materials can include high temperature gaskets, metal alloys, ceramics, clay or mineral liners, composites or other materials which having melting points above typical operating temperatures and act as a continuation of the permeability control provided by walls of the control infrastructure.\|[0064] Further, walls of the constructed infrastructure can be configured to minimize heat loss. In one aspect, the walls can be constructed having a substantially uniform thickness which is optimized to provide sufficient mechanical strength while also minimizing the volume of wall material through which the conduits pass. Specifically, excessively thick walls can reduce the amount of heat which is transferred into the permeable body by absorbing the same through conduction. Conversely, the walls can also act as a thermal barrier to somewhat insulate the permeable body and retain heat therein during operation.\|[0065] In one embodiment, fluid and gas compounds within the permeable body can be altered for desired extractive products using, as an example, induced pressure through gases or piled lithostatic pressure from piled rubble. Thus, some degree of upgrading and/or modification can be accomplished simultaneous with the recovery process. Further, certain hydrocarbonaceous materials can require treatment using specific diluents or other materials. For example, treatment of tar sands can be readily accomplished by steam injection or solvent injection to facilitate separation of bitumen from sand particles according to well known mechanisms.\|[0066] With the above description in mind, FIG. 1 depicts a side view of one embodiment showing an engineered capsule containment and extraction impoundment 100 where existing grade 108 is used primarily as support for the impermeable floor layer 112. Exterior capsule impoundment side walls 102 provide containment and can, but need not be, subdivided by interior walls 104. Subdividing can create separate containment capsules 122 within a greater capsule containment of the impoundment 100 which can be any geometry, size or subdivision. Further subdivisions can be horizontally or vertically stacked. By creating separate containment capsules 122 or chambers, classification of lower grade materials, varied gases, varied liquids, varied process stages, varied enzymes or microbiology types, or other desired and staged processes can be readily accommodated. Sectioned capsules constructed as silos within larger constructed capsules can also be designed to provide staged and sequenced processing, temperatures, gas and fluid compositions and thermal transfers. Such sectioned capsules can provide additional environmental monitoring and can be built of lined and engineered tailings berms similar to the primary exterior walls. In one embodiment, sections within the impoundment 100 can be used to place materials in isolation, in the absence of external heat, or with the intent of limited or controlled combustion or solvent application. Lower content hydrocarbon bearing material can be useful as a combustion material or as fill or a berm wall building material. Material which does not meet a various cut-off grade thresholds can also be sequestered without alteration in an impoundment dedicated for such purpose. In such embodiments, such areas may be completely isolated or bypassed by heat, solvents, gases, liquids, or the like. Optional monitoring devices and/or equipment can be permanently or temporarily installed within the impoundment or outside perimeters of the impoundments in order to verify containment of the sequestered material.\|[0067] Walls 102 and 104 as well as cap 116 and impermeable layer 112 can be engineered and reinforced by gabions 146 and or geogrid 148 layered in fill compaction. Alternatively, these walls 102, 104, 116 and 112 which comprise the permeability control impoundment and collectively define the encapsulated volume can be formed of any other suitable material as previously described. In this embodiment, the impoundment 100 includes side walls 102 and 104 which are self-supporting. In one embodiment, tailings berms, walls, and floors can be compacted and engineered for structure as well as permeability. The use of compacted geogrids and other deadman structures for support of berms and embankments can be included prior to or incorporated with permeability control layers which may include sand, clay, bentonite clay, gravel, cement, grout, reinforced cement, refractory cements, insulations, geo-membranes, drainpipes, temperature resistant insulations of penetrating heated pipes, etc.\|[0068] In one alternative embodiment, the permeability control impoundment can include side walls which are compacted earth and/or undisturbed geological formations while the cap and floors are impermeable. Specifically, in such embodiments an impermeable cap can be used to prevent uncontrolled escape of volatiles and gases from the impoundment such that appropriate gas collection outlets can be used. Similarly, an impermeable floor can be used to contain and direct collected liquids to a suitable outlet such the drain system 133 to remove liquid products from lower regions of the impoundment. Although impermeable side walls can be desirable in some embodiments, such are not always required. In some cases, side walls can be exposed undisturbed earth or compacted fill or earth, or other permeable material. Having permeable side walls may allow some small egress of gases and/or liquids from the impoundment.\|[0069] However, it may be desirable to have the impoundment constructed such that a positive pressure is maintained therein thereby preventing the introduction of air or other oxidizing gases from entering into the impoundment. The presence of oxygen can result in polymerization and gumming of the hydrocarbons and other contents within the impoundment. Further, the presence of oxygen can induce combustion within the system.\|[0070] Although not shown, above, below, around and adjacent to constructed capsule containment vessels environmental hydrology measures can be engineered to redirect surface water away from the capsule walls, floors, caps, etc. during operation. Further, gravity assisted drainage pipes and mechanisms can be utilized to aggregate and channel fluids, liquids or solvents within the encapsulated volume to central gathering, pumping, condensing, heating, staging and discharge pipes, silos, tanks, and/or wells as needed. In a similar manner, steam and/or water which is intentionally introduce, e.g. for tar sands bitumen treatment, can be recycled.\|[0071] Once wall structures 102 and 104 have been constructed above a constructed and impermeable floor layer 112 which commences from ground surface 106, the mined rubble 120 (which may be crushed or classified according to size or hydrocarbon richness), can be placed in layers upon (or next to) placed tubular heating pipes 118, fluid drainage pipes 124, and, or gas gathering or injection pipes 126. These pipes can be oriented and designed in any optimal flow pattern, angle, length, size, volume, intersection, grid, wall sizing, alloy construction, perforation design, injection rate, and extraction rate. In some cases, pipes such as those used for heat transfer can be connected to, recycled through or derive heat from heat source 134. Alternatively, or in combination with, recovered gases can be condensed by a condenser 140. Heat recovered by the condenser can be optionally used to supplement heating of the permeable body or for other process needs.\|[0072] Heat source 134 can derive, amplify, gather, create, combine, separate, transmit or include heat derived from any suitable heat source including, but not limited to, fuel cells (e.g. solid oxide fuel cells, molten carbonate fuel cells and the like), solar sources, wind sources, hydrocarbon liquid or gas combustion heaters, geothermal heat sources, nuclear power plant, coal fired power plant, radio frequency generated heat, wave energy, flameless combustors, natural distributed combustors, or any combination thereof. In some cases, electrical resistive heaters or other heaters can be used, although fuel cells and combustion-based heaters are particularly effective. In some locations, geothermal water can be circulated to the surface in adequate amounts to heat the permeable body and directed into the infrastructure.\|[0073] In another embodiment, electrically conductive material can be distributed throughout the permeable body and an electric current can be passed through the conductive material sufficient to generate heat. The electrically conductive material can include, but is not limited to, metal pieces or beads, conductive cement, metal coated particles, metal-ceramic composites, conductive semi-metal carbides, calcined petroleum coke, laid wire, combinations of these materials, and the like. The electrically conductive material can be premixed having various mesh sizes or the materials can be introduced into the permeable body subsequent to formation of the permeable body.\|[0074] Liquids or gases can transfer heat from heat source 134, or in another embodiment, in the cases of hydrocarbon liquid or gas combustion, radio frequency generators (microwaves), or fuel cells all can, but need not, actually generate heat inside of capsule impoundment area 114 or 122. In one embodiment, heating of the permeable body can be accomplished by convective heating from hydrocarbon combustion. Of particular interest is hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen. Stoichiometric conditions can allow for significantly increased heat gas temperatures. Stoichiometric combustion can employ but does not generally require a pure oxygen source which can be provided by known technologies including, but not limited to, oxygen concentrators, membranes, electrolysis, and the like. In some embodiments oxygen can be provided from air with stoichiometric amounts of oxygen and hydrogen. Combustion off gas can be directed to an ultra-high temperature heat exchanger, e.g. a ceramic or other suitable material having an operating temperature above about 2500° F. Air obtained from ambient or recycled from other processes can be heated via the ultra high temperature heat exchanger and then sent to the impoundment for heating of the permeable body. The combustion off gases can then be sequestered without the need for further separation, i.e. because the off gas is predominantly carbon dioxide and water.\|[0075] In order to minimize heat losses, distances can be minimized between the combustion chamber, heat exchanger and impoundments. Therefore, in one specific detailed embodiment portable combustors can be attached to individual heating conduits or smaller sections of conduits. Portable combustors or burners can individually provide from about 100,000 Btu to about 1,000,000 Btu with about 600,000 Btu per pipe generally being sufficient.\|[0076] Alternatively, in-capsule combustion can be initiated inside of isolated capsules within a primary constructed capsule containment structure. This process partially combusts hydrocarbonaceous material to provide heat and intrinsic pyrolysis. Unwanted air emissions 144 can be captured and sequestered in a formation 108 once derived from capsule containment 114, 122 or from heat source 134 and delivered by a drilled well bore 142. Heat source 134 can also create electricity and transmit, transform or power via electrical transmission lines 150. The liquids or gases extracted from capsule impoundment treatment area 114 or 122 can be stored in a nearby holding tank 136 or within a capsule containment 114 or 122. For example, the impermeable floor layer 112 can include a sloped area 110 which directs liquids towards drain system 133 where liquids are directed to the holding tank.\|[0077] As rubble material 120 is placed with piping 118, 124, 126, and 128, various measurement devices or sensors 130 are envisioned to monitor temperature, pressure, fluids, gases, compositions, heating rates, density, and all other process attributes during the extractive process within, around, or underneath the engineered capsule containment impoundment 100. Such monitoring devices and sensors 130 can be distributed anywhere within, around, part of, connected to, or on top of placed piping 118, 124, 126, and 128 or, on top of, covered by, or buried within rubble material 120 or impermeable barrier zone 112.\|[0078] As placed rubble material 120 fills the capsule treatment area 114 or 122, 120 becomes the ceiling support for engineered impermeable cap barrier zone 138, and wall barrier construction 170, which may include any combination of impermeability and engineered fluid and gas barrier or constructed capsule construction comprising those which may make up 112 including, but not limited to clay 162, compacted fill or import material 164, cement or refractory cement containing material 166, geo synthetic membrane, liner or insulation 168. Above 138, fill material can be oriented as ceiling cap 116 is placed to create lithostatic pressure upon the capsule treatment areas 114 or 122. Covering the permeable body with compacted fill sufficient to create an increased lithostatic pressure within the permeable body can be useful in further increasing hydrocarbon product quality. A compacted fill ceiling can substantially cover the permeable body, while the permeable body in return can substantially support the compacted fill ceiling. The compacted fill ceiling can further be sufficiently impermeable to removed hydrocarbon or an additional layer of permeability control material can be added in a similar manner as side and/or floor walls. Additional pressure can be introduced into extraction capsule treatment area 114 or 122 by increasing any gas or fluid once extracted, treated or recycled, as the case may be, via any of piping 118, 124, 126, or 128. In one embodiment the additional pressure is sufficient to maintain a positive pressure within the treatment area and is provided by the introduction of a non-oxidizing gas such as hydrogen, nitrogen, propane, carbon dioxide or any other gas which provides an inert atmosphere within the treatment area. Other potential flushing gases can include but are not limited to hydrocarbon gases. All relative measurements, optimization rates, injection rates, extraction rates, temperatures, heating rates, flow rates, pressure rates, capacity indicators, chemical compositions, or other data relative to the process of heating, extraction, stabilization, sequestration, impoundment, upgrading, refining or structure analysis within the capsule impoundment 100 are envisioned through connection to a computing device 132 which operates computer software for the management, calculation and optimization of the entire process. Further, core drilling, geological reserve analysis and assay modeling of a formation prior to blasting, mining and hauling (or at any time before, after or during such tasks) can serve as data input feeds into computer controlled mechanisms that operate software to identify optimal placements, dimensions, volumes and designs calibrated and cross referenced to desired production rate, pressure, temperature, heat input rates, gas weight percentages, gas injection compositions, heat capacity, permeability, porosity, chemical and mineral composition, compaction, density. Such analysis and determinations may include other factors like weather data factors such as temperature and air moisture content impacting the overall performance of the constructed infrastructure. Other data such as ore moisture content, hydrocarbon richness, weight, mesh size, and mineral and geological composition can be utilized as inputs including time value of money data sets yielding project cash flows, debt service and internal rates of return.\|[0079] FIG. 2A shows a collection of impoundments including an uncovered or uncapped capsule impoundment 100, containing sectioned capsule impoundments 122 inside of a mining quarry 200 with various elevations of bench mining. FIG. 2B illustrates a single impoundment 122 without associated conduits and other aspects merely for clarity. This impoundment can be similar to that illustrated in FIG. 1 or any other configuration. In some embodiments, it is envisioned that mining rubble can be transferred down chutes 230 or via conveyors 232 to the quarry capsule impoundments 100 and 122 without any need of mining haul trucks.\|[0080] FIG. 3 shows the engineered permeability barriers 112 below capsule impoundment 100 resting on exiting grade 106 of formation 108 with cap covering material or fill 302 on the sides and top of capsule impoundment 100 to ultimately (following the process) cover and reclaim a new earth surface 300. Indigenous plants which may have been temporarily moved from the area may be replanted such as trees 306. The constructed infrastructures can generally be single use structures which can be readily and securely shut down with minimal additional remediation. This can dramatically reduce costs associated with moving large volumes of spent materials. However, in some circumstances the constructed infrastructures can be excavated and reused. Some equipment such as radio frequency (RF) mechanisms, tubulars, devices and emitters may be recovered from within the constructed impoundment upon completion of hydrocarbon recovery.\|[0081] FIG. 4 shows computer means 130 controlling various property inputs and outputs of conduits 118, 126, or 128 connected to heat source 134 during the process among the subdivided impoundments 122 within a collective impoundment 100 to control heating of the permeable body. Similarly, liquid and vapor collected from the impoundments can be monitored and collected in tank 136 and condenser 140, respectively. Condensed liquids from the condenser can be collected in tank 141, while non-condensable vapor collected at unit 143. As described previously, the liquid and vapor products can be combined or more often left as separate products depending on condensability, target product, and the like. A portion of the vapor product can be optionally condensed and combined with the liquid products in tank 136. However, much of the vapor product will be C4 and lighter gases which can be burned, sold or used within the process. For example, hydrogen gas may be recovered using conventional gas separation and used to hydrotreat the liquid products according to conventional upgrading methods, e.g. catalytic, etc. or the non-condensable gaseous product can be burned to produce heat for use in heating the permeable body, heating an adjacent or nearby impoundment, heating service or personnel areas, or satisfying other process heat requirements. The constructed infrastructure can include thermocouples, pressure meters, flow meters, fluid dispersion sensors, richness sensors and any other conventional process control devices distributed throughout the constructed infrastructure. These devices can be each operatively associated with a computer such that heating rates, product flow rates, and pressures can be monitored or altered during heating of the permeable body. Optionally, in-place agitation can be performed using, for example, ultrasonic generators which are associated with the permeable body. Such agitation can facilitate separation and pyrolysis of hydrocarbons from the underlying solid materials with which they are associated. Further, sufficient agitation can reduce clogging and agglomeration throughout the permeable body and the conduits.\|[0082] FIG. 5 shows how any of the conduits can be used to transfer heat in any form of gas, liquid or heat via transfer means 510 from any sectioned capsule impoundment to another. Then, cooled fluid can be conveyed via heat transfer means 512 to the heat originating capsule 500, or heat originating source 134 to pick up more heat from capsule 500 to be again recirculated to a destination capsule 522. Thus, various conduits can be used to transfer heat from one impoundment to another in order to recycle heat and manage energy usage to minimize energy losses.\|[0083] In yet another aspect, a hydrogen donor agent can be introduced into the permeable body during the step of heating. The hydrogen donor agent can be any composition which is capable of hydrogenation of the hydrocarbons and can optionally be a reducing agent. Non-limiting examples of suitable hydrogen donor agents can include synthesis gas, propane, methane, hydrogen, natural gas, natural gas condensate, industrial solvents such as acetones, toluenes, benzenes, xylenes, cumenes, cyclopentanes, cyclohexanes, lower alkenes (C4-C10), terpenes, substituted compounds of these solvents, etc., and the like. Further, the recovered hydrocarbons can be subjected to hydrotreating either within the permeable body or subsequent to collection. Advantageously, hydrogen recovered from the gas products can be reintroduced into the liquid product for upgrading. Regardless, hydrotreating or hydrodesulfurization can be very useful in reducing nitrogen and sulfur content in final hydrocarbon products. Optionally, catalysts can be introduced to facilitate such reactions. In addition, introduction of light hydrocarbons into the permeable body can result in reforming reactions which reduce the molecular weight, while increasing the hydrogen to carbon ratio. This is particularly advantageous due at least in part to high permeability of the permeable body, e.g. often around 30%-40% void volume although void volume can generally vary from about 10% to about 50% void volume. Light hydrocarbons which can be injected can be any which provide reforming to recovered hydrocarbons. Non-limiting examples of suitable light hydrocarbons include natural gas, natural gas condensates, industrial solvents, hydrogen donor agents, and other hydrocarbons having ten or fewer carbons, and often five or fewer carbons. Currently, natural gas is an effective, convenient and plentiful light hydrocarbon. As mentioned previously, various solvents or other additives can also be added to aid in extraction of hydrocarbon products from the oil shale and can often also increase fluidity.\|[0084] The light hydrocarbon can be introduced into the permeable body by conveying the same through a delivery conduit having an open end in fluid communication with a lower portion of the permeable body such that the light hydrocarbons (which are a gas under normal operating conditions) permeate up through the permeable body. Alternatively, this same approach can be applied to recovered hydrocarbons which are first delivered to an empty impoundment. In this way, the impoundment can act as a holding tank for direct products from a nearby impoundment and as a reformer or upgrader. In this embodiment, the impoundment can be at least partially filled with a liquid product where the gaseous light hydrocarbon is passed through and allowed to contact the liquid hydrocarbon products at temperatures and conditions sufficient to achieve reforming in accordance with well known processes. Optional reforming catalysts which include metals such as Pd, Ni or other suitable catalytically active metals can also be included in the liquid product within the impoundment. The addition of catalysts can serve to lower and/or adjust reforming temperature and/or pressure for particular liquid products. Further, the impoundments can be readily formed at almost any depth. Thus, optimal reforming pressures (or recovery pressures when using impoundment depth as pressure control measure for recovery from a permeable body) can be designed based on hydrostatic pressure due to the amount of liquid in the impoundment and the height of the impoundment, i.e. P=ρgh. In addition, the pressure can vary considerably over the height of the impoundment sufficient to provide multiple reforming zones and tailorable pressures. Generally, pressures within the permeable body can be sufficient to achieve substantially only liquid extraction, although some minor volumes of vapor may be produced depending on the particular composition of the permeable body. As a general guideline, pressures can range from about 5 atm to about 50 atm, although pressures from about 6 atm to about 20 atm can be particularly useful. However, any pressure greater than about atmospheric can be used.\|[0085] In certain instances the maintaining of a positive pressure within the enclosed capsule, relative to the outside atmosphere, has certain advantages. For example, a positive pressure prevents unwanted gases from entering into the impoundment during the hydrocarbon removal process and further expedites the removal of hydrocarbons from within the impoundment. Maintaining a positive pressure by means of a non-oxidizing gas reduces the likelihood of unwanted combustion and retards or prevents polymerization of lighter hydrocarbons which can form deposits on pipes or other infrastructure within the impoundment. Also, a positive pressure enables the flushing of the system in the event of certain events or happenings. One example might be in the event there is an interruption of the processing of the hydrocarbonaceous material and the collection of hydrocarbons due to a leak or other unwanted escape of fluids from within the impoundment. A positive pressure allows for the almost instantaneous introduction of non-oxidizing gases at a predetermined temperature, preferably a cooling temperature, to flush hydrocarbons and other vaporous components from the permeable body and within the impoundment so as to maintain an inert environment until any problem is detected and corrected. As previously noted gases such as hydrogen, nitrogen, propane, carbon dioxide, hydrocarbons, and the like can be used to flush the impoundment. Although any functional positive pressure can be suitable, pressure can generally be from about 1.01 atm to about 10 atm, and in one aspect from about 1.1 atm to about 4 atm.\|[0086] Further, once the hydrocarbon production stage is completed, the impoundment can be flushed with a non-oxidizing gas in order to remove further recoverable hydrocarbons from the impoundment. Such flushing can be accomplished in stages or in increments of temperature reduction or any other means to recover meaningful quantities of hydrocarbons. It may be beneficial to allow such flushing and cooling in increments such as to maximize the recovery of hydrocarbons while, at the same time, prepare the hydrocarbon lean shale or other materials, for further processing and/or pacification. The flushing times will obviously depend on the size of the permeable body and the impoundment and can be accomplished in a matter of hours, days or even weeks.\|[0087] Also, the lean shale or other inorganic matter resulting from the termination of the hydrocarbon removal process may still contain other components such as heavy metals, precious metals or other mineral components in the permeable body that can be extracted in further processing steps. Certain deposits may contain radioactive materials that require further processing and/or impounding in order to comply with governmental regulations.\|[0088] In one embodiment, extracted crude has fines precipitated out within the subdivided capsules. Extracted fluids and gases can be treated for the removal of fines and dust particles. Separation of fines from shale oil can be accomplished by techniques such as, but not limited to, hot gas filtering, precipitation, and heavy oil recycling.\|[0089] Hydrocarbon products recovered from the permeable body can be further processed (e.g. refined) or used as produced. Any condensable gaseous products can be condensed by cooling and collection, while non-condensable gases can be collected, burned as fuel, reinjected, or otherwise utilized or disposed of Optionally, mobile equipment can be used to collect gases. These units can be readily oriented proximate to the control infrastructure and the gaseous product directed thereto via suitable conduits from an upper region of the control infrastructure.\|[0090] In yet another alternative embodiment, heat within the permeable body can be recovered subsequent to primary recovery of hydrocarbon materials therefrom. For example, a large amount of heat is retained in the permeable body. In one optional embodiment, the permeable body can be flooded with a heat transfer fluid such as water to form a heated fluid, e.g. heated water and/or steam. At the same time, this process can facilitate removal of some residual hydrocarbon products via a physical rinsing of the spent shale solids. In some cases, the introduction of water and presence of steam can result in water gas shift reactions and formation of synthesis gas. Steam recovered from this process can be used to drive a generator, directed to another nearby infrastructure, or otherwise used. Hydrocarbons and/or synthesis gas can be separated from the steam or heated fluid by conventional methods.\|[0091] Although the methods and infrastructure allow for improved permeability and control of operating conditions, significant quantities of unrecovered hydrocarbons, precious metals, minerals, sodium bicarbonate or other commercially valuable materials often remain in the permeable body. Therefore, a selective solvent can be injected or introduced into the permeable body. Typically, this can be done subsequent to collecting the hydrocarbons, although certain selective solvents can be beneficially used prior to heating and/or collection. This can be done using one or more of the existing conduits or by direct injection and percolation through the permeable body. The selective solvent or leachate can be chosen as a solvent for one or more target materials, e.g. minerals, precious metal, heavy metals, hydrocarbons, or sodium bicarbonate. In one specific embodiment, steam or carbon dioxide can be used as a rinse of the permeable body to dislodge at least a portion of any remaining hydrocarbons. This can be beneficial not only in removing potentially valuable secondary products, but also in cleaning remaining spent materials of trace heavy metal or inorganics to below detectable levels in order to comply with regulatory standards or to prevent inadvertent leaching of materials at a future date.\|[0092] More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body. Typically, such recovery of materials can be performed prior to heat treatment of the permeable body. Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like. For example, heavy metals, bauxite or aluminum, and mercury can be removed by flooding the permeable body with an appropriate solvent and recirculating the resulting leachate through appropriately designed ion exchange resins (e.g. beads, membranes, etc.).\|[0093] Similarly, bioextraction, bio leaching, biorecovery, or bioremediation of hydrocarbon material, spent materials, or precious metals can be performed to further improve remediation, extract valuable metals, and restoration of spent material to environmentally acceptable standards. In such bioextraction scenarios, conduits can be used to inject catalyzing gases as a precursor which helps to encourage bioreaction and growth. Such microorganisms and enzymes can biochemically oxidize the ore body or material or cellulosic or other biomass material prior to an ore solvent extraction via bio-oxidation. For example, a perforated pipe or other mechanism can be used to inject a light hydrocarbon (e.g. methane, ethane, propane or butane) into the permeable body sufficient to stimulate growth and action of native bacteria. Bacteria can be native or introduced and may grow under aerobic or anaerobic conditions. Such bacteria can release metals from the permeable body which can then be recovered via flushing with a suitable solvent or other suitable recovery methods. The recovered metals can then be precipitated out using conventional methods.\|[0094] Synthesis gas can also be recovered from the permeable body during the step of heating. Various stages of gas production can be manipulated through processes which raise or lower operating temperatures within the encapsulated volume and adjust other inputs into the impoundment to produce synthetic gases which can include but are not limited to, carbon monoxide, hydrogen, hydrogen sulfide, hydrocarbons, ammonia, water, nitrogen or various combinations thereof. In one embodiment, temperature and pressure can be controlled within the permeable body to lower CO2 emissions as synthetic gases are extracted.\|[0095] Hydrocarbon product recovered from the constructed infrastructures can most often be further processed, e.g. by upgrading, refining, etc. Sulfur from related upgrading and refining processing can be isolated in various constructed sulfur capsules within the greater structured impoundment capsule. Constructed sulfur capsules can be spent constructed infrastructures or dedicated for the purpose of storage and isolation after desulfurization.\|[0096] Similarly, spent hydrocarbonaceous material remaining in the constructed infrastructure can be utilized in the production of cement and aggregate products for use in construction or stabilization of the infrastructure itself or in the formation of offsite constructed infrastructures. Such cement products made with the spent shale may include, but are not limited to, mixtures with Portland cement, calcium salt, volcanic ash, perlite, synthetic nano carbons, sand, fiber glass, crushed glass, asphalt, tar, binding resins, cellulosic plant fibers, and the like.\|[0097] In still another embodiment, injection, monitoring and production conduits or extraction egresses can be incorporated into any pattern or placement within the constructed infrastructure. Monitoring wells and constructed geo membrane layers beneath or outside of the constructed capsule containment can be employed to monitor unwanted fluid and moisture migration outside of containment boundaries and the constructed infrastructure.\|[0098] Although a filled and prepared constructed infrastructure can often be immediately heated to recover hydrocarbons, this is not required. For example, a constructed infrastructure which is built and filled with mined hydro carbonaceous material can be left in place as a proven reserve. Such structures are less susceptible to explosion or damage due to terrorist activity and can also provide strategic reserves of unprocessed petroleum products, with classified and known properties so that economic valuations can be increased and more predictable. Long term petroleum storage often faces quality deterioration issues over time. Thus, these approaches can optionally be used for long term quality insurance and storage with reduced concerns regarding breakdown and degradation of hydrocarbon products.\|[0099] In still another aspect, the high quality liquid product can be blended with more viscous lower quality (e.g. lower API) hydrocarbon products. For example, kerogen oil produced from the impoundments can be blended with bitumen to form a blended oil. The bitumen is typically not transportable through an extended pipeline under conventional and accepted pipeline standards and can have a viscosity substantially above and an API substantially below that of the kerogen oil. By blending the kerogen oil and bitumen, the blended oil can be rendered transportable without the use of additional diluents or other viscosity or API modifiers. As a result, the blended oil can be pumped through a pipeline without requiring additional treatments to remove a diluent or returning such diluents via a secondary pipeline. Conventionally, bitumen is combined with a diluent such as natural gas condensate or other low molecular weight liquids, to allow pumping to a remote location. The diluent is removed and returned via a second pipeline back to the bitumen source. These approaches allow for elimination of returning diluent and simultaneous upgrading of the bitumen.\|[0100] Although these processes are mining-dependent, they are not limited or encumbered to conventional aboveground (ex-situ) retorting processes. This approach improves upon the benefits of surface retorts including better process control of temperature, pressure, injection rates, fluid and gas compositions, product quality and better permeability due to processing and heating mined rubble. These advantages are available while still addressing the volume, handling, and scalability issues most fabricated surface retorts cannot provide.\|[0101] Other improvements which can be realized are related to environmental protection. Conventional surface retorts have had the problem of spent shale after it has been mined and has passed through a surface retort. Spent shale which has been thermally altered requires special handling to reclaim and isolate from surface drainage basins and underground aquifers. This approach addresses reclamation and retorting in a uniquely combined approach. In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants. This approach uniquely provides solutions to problems for not just one, but many problems, and in an integrated approach. As a result, significant benefits to the public can be achieved in terms of energy production, economic opportunity, environmental stewardship and energy output.\|[0102] It is to be understood that the above-referenced arrangements are illustrative of the application for the principles of the present invention. Thus, while the present invention has been described above in connection with the exemplary embodiments, it will be apparent to those of ordinary skill in the art that numerous modifications and alternative arrangements can be made without departing from the principles and concepts of the invention as set forth in the claims.	(US8349171)\|RELATED APPLICATION\|[0001] This application claims priority to U.S. Provisional Patent Application No. 61/152,146, filed Feb. 12, 2009, which is incorporated herein by reference.\|(US8349171)\|BACKGROUND\|[0002] Global and domestic demand for fossil fuels continues to rise despite price increases and other economic and geopolitical concerns. As such demand continues to rise, research and investigation into finding additional economically viable sources of fossil fuels correspondingly increases. Historically, many have recognized the vast quantities of energy stored in oil shale, coal and tar sand deposits, for example. However, these sources remain a difficult challenge in terms of economically competitive recovery. Canadian tar sands have shown that such efforts can be fruitful, although many challenges still remain, including environmental impact, product quality, production costs and process time, among others.\|[0003] Estimates of world-wide oil shale reserves range from two to almost seven trillion barrels of oil, depending on the estimating source. Regardless, these reserves represent a tremendous volume and remain a substantially untapped resource. A large number of companies and investigators continue to study and test methods of recovering oil from such reserves. In the oil shale industry, methods of extraction have included underground rubble chimneys created by explosions, in-situ methods such as In-Situ Conversion Process (ICP) method (Shell Oil), and heating within steel fabricated retorts. Other methods have included in-situ radio frequency methods (microwaves), and “modified” in-situ processes wherein underground mining, blasting and retorting have been combined to make rubble out of a formation to allow for better heat transfer and product removal.\|[0004] Among typical oil shale processes, all face tradeoffs in economics and environmental concerns. No current process alone satisfies economic, environmental and technical challenges. Moreover, global warming concerns give rise to additional measures to address carbon dioxide (CO2) emissions which are associated with such processes. Methods are needed that accomplish environmental stewardship, yet still provide high-volume cost-effective oil production.\|[0005] Below ground in-situ concepts emerged based on their ability to produce high volumes while avoiding the cost of mining. While the cost savings resulting from avoiding mining can be achieved, the in-situ method requires heating a formation for a longer period of time due to the extremely low thermal conductivity and high specific heat of solid oil shale. Perhaps the most significant challenge for any in-situ process is the uncertainty and long term potential of water contamination that can occur with underground freshwater aquifers. In the case of Shell's ICP method, a “freeze wall” is used as a barrier to keep separation between aquifers and an underground treatment area. Although this is possible, no long term analysis has proven for extended periods to guarantee the prevention of contamination. Without guarantees and with even fewer remedies should a freeze wall fail, other methods are desirable to address such environmental risks.\|[0006] For this and other reasons, the need remains for methods and systems which can provide improved recovery of hydrocarbons from suitable hydrocarbon-containing materials, which have acceptable economics and avoid the drawbacks mentioned above.\|SUMMARY\|[0007] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating the hydrocarbonaceous material can be substantially stationary. Removed fluid hydrocarbons can be collected for further processing, use in the process as supplemental fuel or additives, and/or direct use without further treatment.\|[0008] These systems and processes can allow difficult problems to be solved related to the extraction of hydrocarbon liquids and gases from surface or underground mined hydrocarbon bearing deposits such as oil shale, tar sands, lignite, and coal, and from harvested biomass. Among other things, this approach helps reduce cost, increase volume output, lower air emissions, limit water consumption, prevent underground aquifer contamination, reclaim surface disturbances, reduce material handling costs, remove dirty fine particulates, and improve composition of recovered hydrocarbon liquid or gas. It also addresses water contamination issues with a safer, more predictable, engineered, observable, repairable, adaptable and preventable water protection structure.\|[0009] Additional features and advantages of the invention will be apparent from the following detailed description, which illustrates, by way of example, features of the invention.\|(US8349171)\|BRIEF DESCRIPTION OF THE DRAWINGS\|[0010] FIG. 1 is side partial cutaway view schematic of a constructed permeability control infrastructure in accordance with one embodiment.\|[0011] FIGS. 2A and 2B are top and plan views of a plurality of permeability control impoundments in accordance with one embodiment.\|[0012] FIG. 3 is a side cutaway view of a permeability control impoundment in accordance with one embodiment.\|[0013] FIG. 4 is a schematic of a portion of a constructed infrastructure in accordance with an embodiment.\|[0014] FIG. 5 is a schematic showing heat transfer between two permeability control impoundments in accordance with another embodiment.\|(US8349171)\|DETAILED DESCRIPTION\|[0015] It should be noted that the figures are merely exemplary of several embodiments and no limitations on the scope of the present invention are intended thereby. Further, the figures are generally not drawn to scale, but are drafted for purposes of convenience and clarity in illustrating various aspects of the invention.\|DETAILED DESCRIPTION\|[0016] Reference will now be made to exemplary embodiments and specific language will be used herein to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended. Alterations and further modifications of the inventive features described herein, and additional applications of the principles of the invention as described herein, which would occur to one skilled in the relevant art and having possession of this disclosure, are to be considered within the scope of the invention. Further, before particular embodiments are disclosed and described, it is to be understood that this invention is not limited to the particular process and materials disclosed herein as such may vary to some degree. It is also to be understood that the terminology used herein is used for the purpose of describing particular embodiments only and is not intended to be limiting, as the scope of the present invention will be defined only by the appended claims and equivalents thereof.\|DEFINITIONS\|[0017] In describing and claiming the present invention, the following terminology will be used.\|[0018] The singular forms “a,” “an,” and “the” include plural references unless the context clearly dictates otherwise. Thus, for example, reference to “a wall” includes reference to one or more of such structures, “a permeable body” includes reference to one or more of such materials, and “a heating step” refers to one or more of such steps.\|[0019] As used herein “existing grade” or similar terminology refers to the grade or a plane parallel to the local surface topography of a site containing an infrastructure as described herein which infrastructure may be above or below the existing grade.\|[0020] As used herein, “conduits” refers to any passageway along a specified distance which can be used to transport materials and/or heat from one point to another point. Although conduits can generally be circular pipes, other non-circular conduits can also be useful. Conduits can advantageously be used to either introduce fluids into or extract fluids from the permeable body, convey heat transfer, and/or to transport radio frequency devices, fuel cell mechanisms, resistance heaters, or other devices.\|[0021] As used herein, “constructed infrastructure” refers to a structure which is substantially entirely man made, as opposed to freeze walls, sulfur walls, or other barriers which are formed by modification or filling pores of an existing geological formation.\|[0022] The constructed permeability control infrastructure is often substantially free of undisturbed geological formations, although the infrastructure can be formed adjacent or in direct contact with an undisturbed formation. Such a control infrastructure can be unattached or affixed to an undisturbed formation by mechanical means, chemical means or a combination of such means, e.g. bolted into the formation using anchors, ties, or other suitable hardware.\|[0023] As used herein, “comminuted” refers to breaking a formation or larger mass into pieces. A comminuted mass can be rubbilized or otherwise broken into fragments.\|[0024] As used herein, “hydrocarbonaceous material” refers to any hydrocarbon-containing material from which hydrocarbon products can be extracted or derived. For example, hydrocarbons may be extracted directly as a liquid, removed via solvent extraction, directly vaporized or otherwise removed from the material. However, many hydrocarbonaceous materials contain kerogen or bitumen which is converted to a hydrocarbon through heating and pyrolysis. Hydrocarbonaceous materials can include, but is not limited to, oil shale, tar sands, coal, lignite, bitumen, peat, and other organic materials.\|[0025] As used herein, “impoundment” refers to a structure designed to hold or retain an accumulation of fluid and/or solid moveable materials. An impoundment generally derives at least a substantial portion of foundation and structural support from earthen materials. Thus, the control walls do not always have independent strength or structural integrity apart from the earthen material and/or formation against which they are formed.\|[0026] As used herein, “permeable body” refers to any mass of comminuted hydrocarbonaceous material having a relatively high permeability which exceeds permeability of a solid undisturbed formation of the same composition. Suitable permeable bodies can have greater than about 10% void space and typically have void space from about 30% to 45%, although other ranges may be suitable. Allowing for high permeability facilitates, for example, through the incorporation of large irregularly shaped particles, heating of the body through convection as the primary heat transfer while also substantially reducing costs associated with crushing to very small sizes, e.g. below about 1 to about 0.5 inch.\|[0027] As used herein, “wall” refers to any constructed feature having a permeability control contribution to confining material within an encapsulated volume defined at least in part by control walls. Walls can be oriented in any manner such as vertical, although ceilings, floors and other contours defining the encapsulated volume can also be “walls” as used herein.\|[0028] As used herein, “mined” refers to a material which has been removed or disturbed from an original stratographic or geological location to a second and different location or returned to the same location. Typically, mined material can be produced by rubbilizing, crushing, explosively detonating, or otherwise removing material from a geologic formation.\|[0029] As used herein, “substantially stationary” refers to nearly stationary positioning of materials with a degree of allowance for subsidence, expansion, and/or settling as hydrocarbons are removed from the hydrocarbonaceous material from within the enclosed volume to leave behind lean material. In contrast, any circulation and/or flow of hydrocarbonaceous material such as that found in fluidized beds or rotating retorts involves highly substantial movement and handling of hydro carbonaceous material.\|[0030] As used herein, “substantial” when used in reference to a quantity or amount of a material, or a specific characteristic thereof, refers to an amount that is sufficient to provide an effect that the material or characteristic was intended to provide. The exact degree of deviation allowable may in some cases depend on the specific context. Similarly, “substantially free of” or the like refers to the lack of an identified element or agent in a composition. Particularly, elements that are identified as being “substantially free of” are either completely absent from the composition, or are included only in amounts which are small enough so as to have no measurable effect on the composition.\|[0031] As used herein, “about” refers to a degree of deviation based on experimental error typical for the particular property identified. The latitude provided the term “about” will depend on the specific context and particular property and can be readily discerned by those skilled in the art. The term “about” is not intended to either expand or limit the degree of equivalents which may otherwise be afforded a particular value. Further, unless otherwise stated, the term “about” shall expressly include “exactly,” consistent with the discussion below regarding ranges and numerical data.\|[0032] Concentrations, dimensions, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of about 1 to about 200 should be interpreted to include not only the explicitly recited limits of 1 and 200, but also to include individual sizes such as 2, 3, 4, and sub-ranges such as 10 to 50, 20 to 100, etc.\|[0033] As used herein, a plurality of items, structural elements, compositional elements, and/or materials may be presented in a common list for convenience. However, these lists should be construed as though each member of the list is individually identified as a separate and unique member. Thus, no individual member of such list should be construed as a de facto equivalent of any other member of the same list solely based on their presentation in a common group without indications to the contrary.\|[0034] Recovering Hydrocarbons from Hydrocarbonaceous Materials Under Positive Pressure\|[0035] A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure. This constructed infrastructure defines a substantially encapsulated volume. A mined or harvested hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body of hydrocarbonaceous material. The permeable body can be heated sufficient to remove hydrocarbons therefrom. During heating, the hydrocarbonaceous material is substantially stationary as the constructed infrastructure is a fixed structure. Removed fluid hydrocarbons can be collected for further processing, use in the process, and/or use as recovered.\|[0036] The constructed permeability control infrastructure can be formed using existing grade as floor support and/or as side wall support for the constructed infrastructure. For example, the control infrastructure can be formed as a free standing structure, i.e. using only existing grade as a floor with side walls being man-made. Alternatively, the control infrastructure can be formed within an excavated pit.\|[0037] A constructed permeability control infrastructure can include a permeability control impoundment which defines a substantially encapsulated volume. The permeability control impoundment is substantially free of undisturbed geological formations. Specifically, the permeability control aspect of the impoundment can be completely constructed and manmade as a separate isolation mechanism for prevention of uncontrolled migration of material into or out of the encapsulated volume.\|[0038] In one embodiment, the permeability control impoundment can be formed along walls of an excavated hydrocarbonaceous material deposit. For example, oil shale, tar sands, or coal can be mined from a deposit to form a cavity which corresponds approximately to a desired encapsulation volume for an impoundment. The excavated cavity can then be used as a form and support to create the permeability control impoundment.\|[0039] In one alternative aspect, at least one additional excavated hydrocarbonaceous material deposit can be formed such that a plurality of impoundments can be operated. Further, such a configuration can facilitate a reduction in transportation distance of the mined material. Specifically, the mined hydrocarbonaceous material for any particular encapsulated volume can be mined from an adjacent excavated hydrocarbonaceous material deposit. In this manner, a grid of constructed structures can be built such that mined material can be immediately and directly filled into an adjacent impoundment.\|[0040] Mining and/or excavation of hydro carbonaceous deposits can be accomplished using any suitable technique. Conventional surface mining can be used, although alternative excavators can also be used without requirement of transportation of the mined materials. In one specific embodiment, the hydrocarbonaceous deposit can be excavated using a crane-suspended excavator. One example of a suitable excavator can include vertical tunnel boring machines. Such machines can be configured to excavate rock and material beneath the excavator. As material is removed, the excavator is lowered to ensure substantially continuous contact with a formation. Removed material can be conveyed out of the excavation area using conveyors or lifts. Alternatively, the excavation can occur under aqueous slurry conditions to reduce dust problems and act as a lubricant/coolant. The slurry material can be pumped out of the excavation for separation of solids in a settling tank or other similar solid-liquid separator, or the solids may be allowed to precipitate directly in an impoundment. This approach can be readily integrated with simultaneous or sequential solution-based recovery of metals and other materials as described in more detail below.\|[0041] Further, excavation and formation of a permeability control impoundment can be accomplished simultaneously. For example, an excavator can be configured to remove hydro carbonaceous material while side walls of an impoundment are formed. Material can be removed from just underneath edges of the side walls such that the walls can be guided downward to allow additional wall segments to be stacked above. This approach can allow for increased depths while avoiding or reducing dangers of cave-in prior to formation of supporting impoundment walls.\|[0042] The impoundment can be formed of any suitable material which provides isolation of material transfer across walls of the impoundment. In this manner, integrity of the walls is retained during operation of the control infrastructure sufficient to substantially prevent uncontrolled migration of fluids outside of the control infrastructure. Non-limiting examples of suitable material for use in forming the impoundment of the constructed permeability control infrastructure can include clay, bentonite clay (e.g. clay comprising at least a portion of bentonite), bentonite amended soil, compacted fill, refractory cement, cement, synthetic geogrids, fiberglass, rebar, nanocarbon fullerene additives, filled geotextile bags, polymeric resins, oil resistant PVC liners, or combinations thereof. Engineered cementitious composites (ECC) materials, fiber reinforced composites, and the like can be particularly strong and can be readily engineered to meet permeability and temperature tolerance requirements of a given installation. As a general guideline, materials having low permeability and high mechanical integrity at operating temperatures of the infrastructure can provide good performance, although are not required. For example, materials having a melting point above the maximum operating temperature of the infrastructure can be useful to maintain containment during and after heating and recovery. However, lower temperature materials can also be used if a non-heated buffer zone is maintained between the walls and heated portions of the permeable body. Such buffer zones can range from 6 inches to 50 feet depending on the particular material used for the impoundment and the composition of the permeable body. In another aspect, walls of the impoundment can be acid, water and/or brine resistant, e.g. sufficient to withstand exposure to solvent recovery and/or rinsing with acidic or brine solutions, as well as to steam or water. For impoundment walls formed along formations or other solid support, the impoundment walls can be formed of a sprayed grouting, sprayed liquid emulsions, or other sprayed material such as sprayable refractory grade grouting which forms a seal against the formation and creates the permeability control wall of the impoundments. Impoundment walls may be substantially continuous such that the impoundment defines the encapsulated volume sufficiently to prevent substantial movement of fluids into or out of the impoundment other than defined inlets and outlets, e.g. via conduits or the like as discussed herein. In this manner, the impoundments can readily meet government fluid migration regulations. Alternatively, or in combination with a manufactured barrier, portions of the impoundment walls can be undisturbed geological formation and/or compacted earth. In such cases, the constructed permeability control infrastructure is a combination of permeable and impermeable walls as described in more detail below.\|[0043] In one detailed aspect, a portion of hydrocarbonaceous material, either pre- or post-processed, can be used as a cement fortification and/or cement base which are then poured in place to form portions or the entirety of walls of the control infrastructure. These materials can be formed in place or can be preformed and then assembled on site to form an integral impoundment structure. For example, the impoundment can be constructed by cast forming in place as a monolithic body, extrusion, stacking of preformed or precast pieces, concrete panels joined by a grout (cement, ECC or other suitable material), inflated form, or the like. The forms can be built up against a formation or can be stand alone structures. Forms can be constructed of any suitable material such as, but not limited to, steel, wood, fiberglass, polymer, or the like. The forms can be assembled in place or may be oriented using a crane or other suitable mechanism. Alternatively, the constructed permeability control infrastructure can be formed of gabions and/or geosynthetic fabrics assembled in layers with compacted fill material. Optional binders can be added to enhance compaction of the permeability control walls. In yet another detailed aspect, the control infrastructure can comprise, or consists essentially of, sealant, grout, rebar, synthetic clay, bentonite clay, clay lining, refractory cement, high temperature geomembranes, drain pipes, alloy sheets, or combinations thereof.\|[0044] Impoundment walls can optionally include non-permeable insulation and/or fines collection layers. These permeable layers can be oriented between the permeability control barrier and the permeable body. For example, a layer of hydrocarbonaceous comminuted material can be provided which allows fluids to enter, cool, and at least partially condense within the layer. Such permeable layer material can generally have a particle size smaller than the permeable body. Further, such hydrocarbonaceous material can remove fines from passing fluids via various attractive forces. In one embodiment, the construction of impoundment walls and floors can include multiple compacted layers of indigenous or manipulated low grade shale with any combination of sand, cement, fiber, plant fiber, nano carbons, crushed glass, reinforcement steel, engineered carbon reinforcement grid, calcium salts, and the like. In addition to such composite walls, designs which inhibit long term fluid and gas migration through additional impermeability engineering can be employed including, but not limited to, liners, geo-membranes, compacted soils, imported sand, gravel or rock and gravity drainage contours to move fluids and gases away from impervious layers to egress exits. Impoundment floor and wall construction, can, but need not comprise, a stepped up or stepped down slope or bench as the case of mining course may dictate following the optimal ore grade mining. In any such stepped up or down applications, floor leveling and containment wall construction can typically drain or slope to one side or to a specific central gathering area(s) for removal of fluids by gravity drainage assistance.\|[0045] Optionally, capsule wall and floor construction can include insulation which prevents heat transfer outside of the constructed infrastructure or outside of inner capsules or conduits within the primary constructed capsule containment. Insulation can comprise manufactured materials, cement or various materials other materials which are less thermally conductive than surrounding masses, i.e. permeable body, formation, adjacent infrastructures, etc. Thermally insulating barriers can also be formed within the permeable body, along impoundment walls, ceilings and/or floors. One detailed aspect includes the use of biodegradable insulating materials, e.g. soy insulation and the like. This is consistent with embodiments wherein the impoundment is a single use system such that insulations, pipes, and/or other components can have a relatively low useful life, e.g. less than 1-2 years. This can reduce equipment costs as well as reduce long-term environmental impact.\|[0046] These structures and methods can be applied at almost any scale. Larger encapsulated volumes and increased numbers of impoundments can readily produce hydrocarbon products and performance comparable to or exceeding smaller constructed infrastructures. As an illustration, single impoundments can range in size from tens of meters across to tens of acres. Optimal impoundment sizes may vary depending on the hydrocarbonaceous material and operating parameters, however it is expected that suitable areas can range from about one-half to five acres in top plan surface area.\|[0047] The methods and infrastructures can be used for recovery of hydrocarbons from a variety of hydrocarbonaceous materials. One particular advantage is a wide degree of latitude in controlling particle size, conditions, and composition of the permeable body introduced into the encapsulated volume. Non-limiting examples of mined hydrocarbonaceous material which can be treated comprise oil shale, tar sands, coal, lignite, bitumen, peat, or combinations thereof. In some cases it can be desirable to provide a single type of hydrocarbonaceous material so that the permeable body consists essentially of one of the above materials. However, the permeable body can include mixtures of these materials such that grade, oil content, hydrogen content, permeability and the like can be adjusted to achieve a desired result. Further, different hydrocarbon materials can be placed in multiple layers or in a mixed fashion such as combining coal, oil shale, tar sands, biomass, and/or peat.\|[0048] In one embodiment, hydrocarbon containing material can be classified into various inner capsules within a primary constructed infrastructure for optimization reasons. For instance, layers and depths of mined oil shale formations may be richer in certain depth pay zones as they are mined. Once, blasted, mined, shoveled and hauled inside of capsule for placement, richer oil bearing ores can be classified or mixed by richness for optimal yields, faster recovery, or for optimal averaging within each impoundment. Further, providing layers of differing composition can have added benefits. For example, a lower layer of tar sands can be oriented below an upper layer of oil shale. Generally, the upper and lower layers can be in direct contact with one another although this is not required. The upper layer can include heating pipes embedded therein as described in more detail below. The heating pipes can heat the oil shale sufficient to liberate kerogen oil, including short-chain liquid hydrocarbons, which can act as a solvent for bitumen removal from the tar sands. In this manner, the upper layer acts as an in situ solvent source for enhancing bitumen removal from the lower layer. Heating pipes within the lower layer are optional such that the lower layer can be free of heating pipes or may include heating pipes, depending on the amount of heat transferred via downward passing liquids from the upper layer and any other heat sources. The ability to selectively control the characteristics and composition of the permeable body adds a significant amount of freedom in optimizing oil yields and quality.\|[0049] Furthermore, in many embodiments, the liberated gaseous and liquid products act as an in situ produced solvent which supplements kerogen removal and/or additional hydrocarbon removal from the hydro carbonaceous material.\|[0050] In yet another detailed aspect, the permeable body can further comprise an additive or biomass. Additives can include any composition which acts to increase the quality of removed hydrocarbons, e.g. increased API, decreased viscosity, improved flow properties, reduced wetting of residual shale, reduction of sulfur, hydrogenation agents, etc. Non-limiting examples of suitable additives can include bitumen, kerogen, propane, natural gas, natural gas condensate, crude oil, refining bottoms, asphaltenes, common solvents, other diluents, and combinations of these materials. In one specific embodiment, the additive can include a flow improvement agent and/or a hydrogen donor agent. Some materials can act as both or either agents to improve flow or as a hydrogen donor. Non-limiting examples of such additives can include methane, natural gas condensates, common solvent such as acetone, toluene, benzene, etc., and other additives listed above. Additives can act to increase the hydrogen to carbon ratio in any hydrocarbon products, as well as act as a flow enhancement agent. For example, various solvents and other additives can create a physical mixture which has a reduced viscosity and/or reduced affinity for particulate solids, rock and the like. Further, some additives can chemically react with hydrocarbons and/or allow liquid flow of the hydrocarbon products. Any additives used can become part of a final recovered product or can be removed and reused or otherwise disposed of.\|[0051] Similarly, biological hydroxylation of hydrocarbonaceous materials to form synthetic gas or other lighter weight products can be accomplished using known additives and approaches. Enzymes or biocatalysts can also be used in a similar manner. Further, manmade materials can also be used as additives such as, but not limited to, tires, polymeric refuse, or other hydrocarbon-containing materials.\|[0052] Although these methods are broadly applicable, as a general guideline, the permeable body can include particles from about ⅛ inch to about 6 feet in largest dimension, and in some cases less than 1 foot and in other cases less than about 6 inches. However, as a practical matter, sizes from about 2 inches to about 2 feet can provide good results with about 1 foot diameter being useful for oil shale especially. Void space can be an important factor in determining optimal particle diameters. As a general matter, any functional void space can be used; however, about 10% to about 50% and in some cases about 30% to about 45% usually provides a good balance of permeability and effective use of available volumes. Void volumes can be varied somewhat by varying other parameters such as heating conduit placement, additives, and the like. Mechanical separation of mined hydrocarbonaceous materials allows creation of fine mesh, high permeability particles which enhance thermal dispersion rates once placed in capsule within the impoundment. The added permeability allows for more reasonable, low temperatures which also help to avoid higher temperatures which result in greater CO2 production from carbonate decomposition and associated release of trace heavy metals, volatile organics, and other compounds which can create toxic effluent and/or undesirable materials which can be monitored and controlled.\|[0053] In one embodiment, computer assisted mining, mine planning, hauling, blasting, assay, loading, transport, placement, and dust control measures can be utilized to fill and optimize the speed of mined material movement into the constructed capsule containment structure. In one alternative aspect, the impoundments can be formed in excavated volumes of a hydrocarbonaceous formation, although other locations remote from the control infrastructure can also be useful. For example, some hydrocarbonaceous formations have relatively thin hydrocarbon-rich layers, e.g. less than about 300 feet thick. Therefore, vertical mining and drilling tend to not be cost effective. In such cases, horizontal mining can be useful to recover the hydrocarbonaceous materials for formation of the permeable body. Although horizontal mining continues to be a challenging endeavor, a number of technologies have been developed and continue to be developed which can be useful in connection with the impoundments. In such cases, at least a portion of the impoundment can be formed across a horizontal layer, while other portions of the impoundment can be formed along and/or adjacent non-hydrocarbon bearing formation layers. Other mining approaches such as, but not limited to, room and pillar mining can provide an effective source of hydrocarbonaceous material with minimal waste and/or reclamation which can be transported to an impoundment and treated in accordance with these principles.\|[0054] As mentioned herein, these systems and processes allow for a large degree of control regarding properties and characteristics of the permeable body which can be designed and optimized for a given installation. Impoundments, individually and across a plurality of impoundments can be readily tailored and classified based on varying composition of materials, intended products and the like. For example, several impoundments can be dedicated to production of heavy crude oil, while others can be configured for production of lighter products and/or syn gas. Non-limiting example of potential classifications and factors can include catalyst activity, enzymatic reaction for specific products, aromatic compounds, hydrogen content, microorganism strain or purpose, upgrading process, target final product, pressure (effects product quality and type), temperature, swelling behavior, aquathermal reactions, hydrogen donor agents, heat superdisposition, garbage impoundment, sewage impoundment, reusable pipes, and others. Typically, a plurality of these factors can be used to configure impoundments in a given project area for distinct products and purposes.\|[0055] The comminuted hydrocarbonaceous material can be filled into the control infrastructure to form the permeable body in any suitable manner. Typically the comminuted hydrocarbonaceous material can be conveyed into the control infrastructure by dumping, conveyors or other suitable approaches. As mentioned previously, the permeable body can have a suitably high void volume. Indiscriminate dumping can result in excessive compaction and reduction of void volumes. Thus, the permeable body can be formed by low compaction conveying of the hydrocarbonaceous material into the infrastructure. For example, retracting conveyors can be used to deliver the material near a top surface of the permeable body as it is formed. In this way, the hydrocarbonaceous material can retain a significant void volume between particles without substantial further crushing or compaction despite some small degree of compaction which often results from lithostatic pressure as the permeable body is formed.\|[0056] Once a desired permeable body has been formed within the control infrastructure, heat can be introduced sufficient to begin removal of hydrocarbons, e.g. via pyrolysis. A suitable heat source can be thermally associated with the permeable body. Optimal operating temperatures within the permeable body can vary depending on the composition and desired products. However, as a general guideline, operating temperatures can range from about 200° F. to about 750° F. Temperature variations throughout the encapsulated volume can vary and may reach as high as 900° F. or more in some areas. In one embodiment, the operating temperature can be a relatively lower temperature to facilitate production of liquid product such as from about 200° F. to about 650° F. This heating step can be a roasting operation which results in beneficiation of the crushed ore of the permeable body. Further, one embodiment comprises controlling the temperature, pressure and other variables sufficient to produce predominantly, and in some cases substantially only, liquid product. Generally, products can include both liquid and gaseous products, while liquid products can require fewer processing steps such as scrubbers etc. The relatively high permeability of the permeable body allows for production of liquid hydrocarbon products and minimization of gaseous products, depending to some extent on the particular starting materials and operating conditions. In one embodiment, the recovery of hydrocarbon products can occur substantially in the absence of cracking within the permeable body.\|[0057] In one aspect, heat can be transferred to the permeable body via convection. Heated gases can be injected into the control infrastructure such that the permeable body is primarily heated via convection as the heated gases pass throughout the permeable body. Heated gases can be produced by combustion of natural gas, hydrocarbon product, or any other suitable source. The heated gases can be imported from external sources or recovered from the process.\|[0058] Alternatively, or in combination with convective heating, a highly configurable approach can include embedding a plurality of conduits within the permeable body. The conduits can be configured for use as heating pipes, cooling pipes, heat transfer pipes, drainage pipes, or gas pipes. Further, the conduits can be dedicated to a single function or may serve multiple functions during operation of the infrastructure, i.e. heat transfer and drainage. The conduits can be formed of any suitable material, depending on the intended function. Non-limiting examples of suitable materials can include clay pipes, refractory cement pipes, refractory ECC pipes, poured in place pipes, metal pipes such as cast iron, stainless steel etc., polymer such as PVC, and the like. In one specific embodiment, all or at least a portion of the embedded conduits can comprise a degradable material. For example, non-galvanized 6″ cast iron pipes can be effectively used for single use embodiments and perform well over the useful life of the impoundment, typically less than about 2 years. Further, different portions of the plurality of conduits can be formed of different materials. Poured in place pipes can be especially useful for very large encapsulation volumes where pipe diameters exceed several feet. Such pipes can be formed using flexible wraps which retain a viscous fluid in an annular shape. For example, PVC pipes can be used as a portion of a form along with flexible wraps, where concrete or other viscous fluid is pumped into an annular space between the PVC and flexible wrap. Depending on the intended function, perforations or other apertures can be made in the conduits to allow fluids to flow between the conduits and the permeable body. Typical operating temperatures exceed the melting point of conventional polymer and resin pipes. In some embodiments, the conduits can be placed and oriented such that the conduits intentionally melt or otherwise degrade during operation of the infrastructure.\|[0059] The plurality of conduits can be readily oriented in any configuration, whether substantially horizontal, vertical, slanted, branched, or the like. At least a portion of the conduits can be oriented along predetermined pathways prior to embedding the conduits within the permeable body. The predetermined pathways can be designed to improve heat transfer, gas-liquid-solid contacting, maximize fluid delivery or removal from specific regions within the encapsulated volume, or the like. Further, at least a portion the conduits can be dedicated to heating of the permeable body. These heating conduits can be selectively perforated to allow heated gases or other fluids to convectively heat and mix throughout the permeable body. The perforations can be located and sized to optimize even and/or controlled heating throughout the permeable body. Alternatively, the heating conduits can form a closed loop such that heating gases or fluids are segregated from the permeable body. Thus, a “closed loop” does not necessarily require recirculation, rather isolation of heating fluid from the permeable body. In this manner, heating can be accomplished primarily or substantially only through thermal conduction across the conduit walls from the heating fluids into the permeable body. Heating in a closed loop allows for prevention of mass transfer between the heating fluid and permeable body and can reduce formation and/or extraction of gaseous hydrocarbon products.\|[0060] During the heating or roasting of the permeable body, localized areas of heat which exceed parent rock decomposition temperatures, often above about 900° F., can reduce yields and form carbon dioxide and undesirable contaminating compounds which can lead to leachates containing heavy metals, soluble organics and the like. The heating conduits can allow for substantial elimination of such localized hot spots while maintaining a vast majority of the permeable body within a desired temperature range. The degree of uniformity in temperature can be a balance of cost (e.g. for additional heating conduits) versus yields. However, at least about 85% of the permeable body can readily be maintained within about 5-10% of a target temperature range with substantially no hot spots, i.e. exceeding the decomposition temperature of the hydrocarbonaceous materials such as about 800° F. and in many cases about 900° F. Thus, operated as described herein, the systems can allow for recovery of hydrocarbons while eliminating or substantially avoiding production of undesirable leachates. Although products can vary considerably depending on the starting materials, high quality liquid and gaseous products are possible. In accordance with one embodiment, a crushed oil shale material can produce a liquid product having an API from about 30 to about 45, with about 33 to about 38 being currently typical, directly from the oil shale without additional treatment. Interestingly, practice of these principles has led to an understanding that pressure appears to be a much less influential factor on the quality of recovered hydrocarbons than temperature and heating times. Although heating times can vary considerably, depending on void space, permeable body composition, quality, etc., as a general guideline times can range from a few days (i.e. 3-4 days) up to about one year. In one specific example, heating times can range from about 2 weeks to about 4 months. Under-heating oil shale at short residence times, i.e. minutes to several hours, can lead to formation of leachable and/or somewhat volatile hydrocarbons. Accordingly, these systems and processes allow for extended residence times at moderate temperatures such that organics present in oil shale can be volatilized and/or carbonized, leaving insubstantial leachable organics. In addition, the underlying shale is not generally decomposed or altered which reduces soluble salt formation.\|[0061] Further, conduits can be oriented among a plurality of impoundments and/or control infrastructures to transfer fluids and/or heat between the structures. The conduits can be welded to one another using conventional welding or the like. Further, the conduits can include junctions which allow for rotation and or small amounts of movement during expansion and subsidence of material in the permeable body. Additionally, the conduits can include a support system which acts to support the assembly of conduits prior to and during filling of the encapsulated volume, as well as during operation. For example, during heating flows of fluids, heating and the like can cause expansion (fracturing or popcorn effect) or subsidence sufficient to create potentially damaging stress and strain on the conduits and associated junctions. A truss support system or other similar anchoring members can be useful in reducing damage to the conduits. The anchoring members can include cement blocks, 1-beams, rebar, columns, etc. which can be associated with walls of the impoundment, including side walls, floors and ceilings.\|[0062] Alternatively, the conduits can be completely constructed and assembled prior to introduction of any mined materials into the encapsulated volume. Care and planning can be considered in designing the predetermined pathways of the conduits and method of filling the volume in order to prevent damage to the conduits during the filling process as the conduits are buried. Thus, as a general rule, the conduits used are oriented ab initio, or prior to embedding in the permeable body such that they are non-drilled. As a result, construction of the conduits and placement thereof can be performed without extensive core drilling and/or complicated machinery associated with well-bore or horizontal drilling. Rather, horizontal or any other orientation of conduit can be readily achieved by assembling the desired predetermined pathways prior to, or contemporaneous with, filling the infrastructure with the mined hydrocarbonaceous material. The non-drilled, hand/crane-placed conduits oriented in various geometric patterns can be laid with valve controlled connecting points which yield precise and closely monitored heating within the capsule impoundment. The ability to place and layer conduits including connecting, bypass and flow valves, and direct injection and exit points, allow for precision temperature and heating rates, precision pressure and pressurization rates, and precision fluid and gas ingress, egress and composition admixtures. For example, when a bacteria, enzyme, or other biological material is used, optimal temperatures can be readily maintained throughout the permeable body to increase performance, reaction, and reliability of such biomaterials.\|[0063] The conduits will generally pass through walls of the constructed infrastructure at various points. Due to temperature differences and tolerances, it can be beneficial to include an insulating material at the interface between the wall and the conduits. The dimensions of this interface can be minimized while also allowing space for thermal expansion differences during startup, steady-state operation, fluctuating operating conditions, and shutdown of the infrastructure. The interface can also involve insulating materials and sealant devices which prevent uncontrolled egress of hydrocarbons or other materials from the control infrastructure. Non-limiting examples of suitable materials can include high temperature gaskets, metal alloys, ceramics, clay or mineral liners, composites or other materials which having melting points above typical operating temperatures and act as a continuation of the permeability control provided by walls of the control infrastructure.\|[0064] Further, walls of the constructed infrastructure can be configured to minimize heat loss. In one aspect, the walls can be constructed having a substantially uniform thickness which is optimized to provide sufficient mechanical strength while also minimizing the volume of wall material through which the conduits pass. Specifically, excessively thick walls can reduce the amount of heat which is transferred into the permeable body by absorbing the same through conduction. Conversely, the walls can also act as a thermal barrier to somewhat insulate the permeable body and retain heat therein during operation.\|[0065] In one embodiment, fluid and gas compounds within the permeable body can be altered for desired extractive products using, as an example, induced pressure through gases or piled lithostatic pressure from piled rubble. Thus, some degree of upgrading and/or modification can be accomplished simultaneous with the recovery process. Further, certain hydrocarbonaceous materials can require treatment using specific diluents or other materials. For example, treatment of tar sands can be readily accomplished by steam injection or solvent injection to facilitate separation of bitumen from sand particles according to well known mechanisms.\|[0066] With the above description in mind, FIG. 1 depicts a side view of one embodiment showing an engineered capsule containment and extraction impoundment 100 where existing grade 108 is used primarily as support for the impermeable floor layer 112. Exterior capsule impoundment side walls 102 provide containment and can, but need not be, subdivided by interior walls 104. Subdividing can create separate containment capsules 122 within a greater capsule containment of the impoundment 100 which can be any geometry, size or subdivision. Further subdivisions can be horizontally or vertically stacked. By creating separate containment capsules 122 or chambers, classification of lower grade materials, varied gases, varied liquids, varied process stages, varied enzymes or microbiology types, or other desired and staged processes can be readily accommodated. Sectioned capsules constructed as silos within larger constructed capsules can also be designed to provide staged and sequenced processing, temperatures, gas and fluid compositions and thermal transfers. Such sectioned capsules can provide additional environmental monitoring and can be built of lined and engineered tailings berms similar to the primary exterior walls. In one embodiment, sections within the impoundment 100 can be used to place materials in isolation, in the absence of external heat, or with the intent of limited or controlled combustion or solvent application. Lower content hydrocarbon bearing material can be useful as a combustion material or as fill or a berm wall building material. Material which does not meet a various cut-off grade thresholds can also be sequestered without alteration in an impoundment dedicated for such purpose. In such embodiments, such areas may be completely isolated or bypassed by heat, solvents, gases, liquids, or the like. Optional monitoring devices and/or equipment can be permanently or temporarily installed within the impoundment or outside perimeters of the impoundments in order to verify containment of the sequestered material.\|[0067] Walls 102 and 104 as well as cap 116 and impermeable layer 112 can be engineered and reinforced by gabions 146 and or geogrid 148 layered in fill compaction. Alternatively, these walls 102, 104, 116 and 112 which comprise the permeability control impoundment and collectively define the encapsulated volume can be formed of any other suitable material as previously described. In this embodiment, the impoundment 100 includes side walls 102 and 104 which are self-supporting. In one embodiment, tailings berms, walls, and floors can be compacted and engineered for structure as well as permeability. The use of compacted geogrids and other deadman structures for support of berms and embankments can be included prior to or incorporated with permeability control layers which may include sand, clay, bentonite clay, gravel, cement, grout, reinforced cement, refractory cements, insulations, geo-membranes, drainpipes, temperature resistant insulations of penetrating heated pipes, etc.\|[0068] In one alternative embodiment, the permeability control impoundment can include side walls which are compacted earth and/or undisturbed geological formations while the cap and floors are impermeable. Specifically, in such embodiments an impermeable cap can be used to prevent uncontrolled escape of volatiles and gases from the impoundment such that appropriate gas collection outlets can be used. Similarly, an impermeable floor can be used to contain and direct collected liquids to a suitable outlet such the drain system 133 to remove liquid products from lower regions of the impoundment. Although impermeable side walls can be desirable in some embodiments, such are not always required. In some cases, side walls can be exposed undisturbed earth or compacted fill or earth, or other permeable material. Having permeable side walls may allow some small egress of gases and/or liquids from the impoundment.\|[0069] However, it may be desirable to have the impoundment constructed such that a positive pressure is maintained therein thereby preventing the introduction of air or other oxidizing gases from entering into the impoundment. The presence of oxygen can result in polymerization and gumming of the hydrocarbons and other contents within the impoundment. Further, the presence of oxygen can induce combustion within the system.\|[0070] Although not shown, above, below, around and adjacent to constructed capsule containment vessels environmental hydrology measures can be engineered to redirect surface water away from the capsule walls, floors, caps, etc. during operation. Further, gravity assisted drainage pipes and mechanisms can be utilized to aggregate and channel fluids, liquids or solvents within the encapsulated volume to central gathering, pumping, condensing, heating, staging and discharge pipes, silos, tanks, and/or wells as needed. In a similar manner, steam and/or water which is intentionally introduce, e.g. for tar sands bitumen treatment, can be recycled.\|[0071] Once wall structures 102 and 104 have been constructed above a constructed and impermeable floor layer 112 which commences from ground surface 106, the mined rubble 120 (which may be crushed or classified according to size or hydrocarbon richness), can be placed in layers upon (or next to) placed tubular heating pipes 118, fluid drainage pipes 124, and, or gas gathering or injection pipes 126. These pipes can be oriented and designed in any optimal flow pattern, angle, length, size, volume, intersection, grid, wall sizing, alloy construction, perforation design, injection rate, and extraction rate. In some cases, pipes such as those used for heat transfer can be connected to, recycled through or derive heat from heat source 134. Alternatively, or in combination with, recovered gases can be condensed by a condenser 140. Heat recovered by the condenser can be optionally used to supplement heating of the permeable body or for other process needs.\|[0072] Heat source 134 can derive, amplify, gather, create, combine, separate, transmit or include heat derived from any suitable heat source including, but not limited to, fuel cells (e.g. solid oxide fuel cells, molten carbonate fuel cells and the like), solar sources, wind sources, hydrocarbon liquid or gas combustion heaters, geothermal heat sources, nuclear power plant, coal fired power plant, radio frequency generated heat, wave energy, flameless combustors, natural distributed combustors, or any combination thereof. In some cases, electrical resistive heaters or other heaters can be used, although fuel cells and combustion-based heaters are particularly effective. In some locations, geothermal water can be circulated to the surface in adequate amounts to heat the permeable body and directed into the infrastructure.\|[0073] In another embodiment, electrically conductive material can be distributed throughout the permeable body and an electric current can be passed through the conductive material sufficient to generate heat. The electrically conductive material can include, but is not limited to, metal pieces or beads, conductive cement, metal coated particles, metal-ceramic composites, conductive semi-metal carbides, calcined petroleum coke, laid wire, combinations of these materials, and the like. The electrically conductive material can be premixed having various mesh sizes or the materials can be introduced into the permeable body subsequent to formation of the permeable body.\|[0074] Liquids or gases can transfer heat from heat source 134, or in another embodiment, in the cases of hydrocarbon liquid or gas combustion, radio frequency generators (microwaves), or fuel cells all can, but need not, actually generate heat inside of capsule impoundment area 114 or 122. In one embodiment, heating of the permeable body can be accomplished by convective heating from hydrocarbon combustion. Of particular interest is hydrocarbon combustion performed under stoichiometric conditions of fuel to oxygen. Stoichiometric conditions can allow for significantly increased heat gas temperatures. Stoichiometric combustion can employ but does not generally require a pure oxygen source which can be provided by known technologies including, but not limited to, oxygen concentrators, membranes, electrolysis, and the like. In some embodiments oxygen can be provided from air with stoichiometric amounts of oxygen and hydrogen. Combustion off gas can be directed to an ultra-high temperature heat exchanger, e.g. a ceramic or other suitable material having an operating temperature above about 2500° F. Air obtained from ambient or recycled from other processes can be heated via the ultra high temperature heat exchanger and then sent to the impoundment for heating of the permeable body. The combustion off gases can then be sequestered without the need for further separation, i.e. because the off gas is predominantly carbon dioxide and water.\|[0075] In order to minimize heat losses, distances can be minimized between the combustion chamber, heat exchanger and impoundments. Therefore, in one specific detailed embodiment portable combustors can be attached to individual heating conduits or smaller sections of conduits. Portable combustors or burners can individually provide from about 100,000 Btu to about 1,000,000 Btu with about 600,000 Btu per pipe generally being sufficient.\|[0076] Alternatively, in-capsule combustion can be initiated inside of isolated capsules within a primary constructed capsule containment structure. This process partially combusts hydrocarbonaceous material to provide heat and intrinsic pyrolysis. Unwanted air emissions 144 can be captured and sequestered in a formation 108 once derived from capsule containment 114, 122 or from heat source 134 and delivered by a drilled well bore 142. Heat source 134 can also create electricity and transmit, transform or power via electrical transmission lines 150. The liquids or gases extracted from capsule impoundment treatment area 114 or 122 can be stored in a nearby holding tank 136 or within a capsule containment 114 or 122. For example, the impermeable floor layer 112 can include a sloped area 110 which directs liquids towards drain system 133 where liquids are directed to the holding tank.\|[0077] As rubble material 120 is placed with piping 118, 124, 126, and 128, various measurement devices or sensors 130 are envisioned to monitor temperature, pressure, fluids, gases, compositions, heating rates, density, and all other process attributes during the extractive process within, around, or underneath the engineered capsule containment impoundment 100. Such monitoring devices and sensors 130 can be distributed anywhere within, around, part of, connected to, or on top of placed piping 118, 124, 126, and 128 or, on top of, covered by, or buried within rubble material 120 or impermeable barrier zone 112.\|[0078] As placed rubble material 120 fills the capsule treatment area 114 or 122, 120 becomes the ceiling support for engineered impermeable cap barrier zone 138, and wall barrier construction 170, which may include any combination of impermeability and engineered fluid and gas barrier or constructed capsule construction comprising those which may make up 112 including, but not limited to clay 162, compacted fill or import material 164, cement or refractory cement containing material 166, geo synthetic membrane, liner or insulation 168. Above 138, fill material can be oriented as ceiling cap 116 is placed to create lithostatic pressure upon the capsule treatment areas 114 or 122. Covering the permeable body with compacted fill sufficient to create an increased lithostatic pressure within the permeable body can be useful in further increasing hydrocarbon product quality. A compacted fill ceiling can substantially cover the permeable body, while the permeable body in return can substantially support the compacted fill ceiling. The compacted fill ceiling can further be sufficiently impermeable to removed hydrocarbon or an additional layer of permeability control material can be added in a similar manner as side and/or floor walls. Additional pressure can be introduced into extraction capsule treatment area 114 or 122 by increasing any gas or fluid once extracted, treated or recycled, as the case may be, via any of piping 118, 124, 126, or 128. In one embodiment the additional pressure is sufficient to maintain a positive pressure within the treatment area and is provided by the introduction of a non-oxidizing gas such as hydrogen, nitrogen, propane, carbon dioxide or any other gas which provides an inert atmosphere within the treatment area. Other potential flushing gases can include but are not limited to hydrocarbon gases. All relative measurements, optimization rates, injection rates, extraction rates, temperatures, heating rates, flow rates, pressure rates, capacity indicators, chemical compositions, or other data relative to the process of heating, extraction, stabilization, sequestration, impoundment, upgrading, refining or structure analysis within the capsule impoundment 100 are envisioned through connection to a computing device 132 which operates computer software for the management, calculation and optimization of the entire process. Further, core drilling, geological reserve analysis and assay modeling of a formation prior to blasting, mining and hauling (or at any time before, after or during such tasks) can serve as data input feeds into computer controlled mechanisms that operate software to identify optimal placements, dimensions, volumes and designs calibrated and cross referenced to desired production rate, pressure, temperature, heat input rates, gas weight percentages, gas injection compositions, heat capacity, permeability, porosity, chemical and mineral composition, compaction, density. Such analysis and determinations may include other factors like weather data factors such as temperature and air moisture content impacting the overall performance of the constructed infrastructure. Other data such as ore moisture content, hydrocarbon richness, weight, mesh size, and mineral and geological composition can be utilized as inputs including time value of money data sets yielding project cash flows, debt service and internal rates of return.\|[0079] FIG. 2A shows a collection of impoundments including an uncovered or uncapped capsule impoundment 100, containing sectioned capsule impoundments 122 inside of a mining quarry 200 with various elevations of bench mining. FIG. 2B illustrates a single impoundment 122 without associated conduits and other aspects merely for clarity. This impoundment can be similar to that illustrated in FIG. 1 or any other configuration. In some embodiments, it is envisioned that mining rubble can be transferred down chutes 230 or via conveyors 232 to the quarry capsule impoundments 100 and 122 without any need of mining haul trucks.\|[0080] FIG. 3 shows the engineered permeability barriers 112 below capsule impoundment 100 resting on exiting grade 106 of formation 108 with cap covering material or fill 302 on the sides and top of capsule impoundment 100 to ultimately (following the process) cover and reclaim a new earth surface 300. Indigenous plants which may have been temporarily moved from the area may be replanted such as trees 306. The constructed infrastructures can generally be single use structures which can be readily and securely shut down with minimal additional remediation. This can dramatically reduce costs associated with moving large volumes of spent materials. However, in some circumstances the constructed infrastructures can be excavated and reused. Some equipment such as radio frequency (RF) mechanisms, tubulars, devices and emitters may be recovered from within the constructed impoundment upon completion of hydrocarbon recovery.\|[0081] FIG. 4 shows computer means 130 controlling various property inputs and outputs of conduits 118, 126, or 128 connected to heat source 134 during the process among the subdivided impoundments 122 within a collective impoundment 100 to control heating of the permeable body. Similarly, liquid and vapor collected from the impoundments can be monitored and collected in tank 136 and condenser 140, respectively. Condensed liquids from the condenser can be collected in tank 141, while non-condensable vapor collected at unit 143. As described previously, the liquid and vapor products can be combined or more often left as separate products depending on condensability, target product, and the like. A portion of the vapor product can be optionally condensed and combined with the liquid products in tank 136. However, much of the vapor product will be C4 and lighter gases which can be burned, sold or used within the process. For example, hydrogen gas may be recovered using conventional gas separation and used to hydrotreat the liquid products according to conventional upgrading methods, e.g. catalytic, etc. or the non-condensable gaseous product can be burned to produce heat for use in heating the permeable body, heating an adjacent or nearby impoundment, heating service or personnel areas, or satisfying other process heat requirements. The constructed infrastructure can include thermocouples, pressure meters, flow meters, fluid dispersion sensors, richness sensors and any other conventional process control devices distributed throughout the constructed infrastructure. These devices can be each operatively associated with a computer such that heating rates, product flow rates, and pressures can be monitored or altered during heating of the permeable body. Optionally, in-place agitation can be performed using, for example, ultrasonic generators which are associated with the permeable body. Such agitation can facilitate separation and pyrolysis of hydrocarbons from the underlying solid materials with which they are associated. Further, sufficient agitation can reduce clogging and agglomeration throughout the permeable body and the conduits.\|[0082] FIG. 5 shows how any of the conduits can be used to transfer heat in any form of gas, liquid or heat via transfer means 510 from any sectioned capsule impoundment to another. Then, cooled fluid can be conveyed via heat transfer means 512 to the heat originating capsule 500, or heat originating source 134 to pick up more heat from capsule 500 to be again recirculated to a destination capsule 522. Thus, various conduits can be used to transfer heat from one impoundment to another in order to recycle heat and manage energy usage to minimize energy losses.\|[0083] In yet another aspect, a hydrogen donor agent can be introduced into the permeable body during the step of heating. The hydrogen donor agent can be any composition which is capable of hydrogenation of the hydrocarbons and can optionally be a reducing agent. Non-limiting examples of suitable hydrogen donor agents can include synthesis gas, propane, methane, hydrogen, natural gas, natural gas condensate, industrial solvents such as acetones, toluenes, benzenes, xylenes, cumenes, cyclopentanes, cyclohexanes, lower alkenes (C4-C10), terpenes, substituted compounds of these solvents, etc., and the like. Further, the recovered hydrocarbons can be subjected to hydrotreating either within the permeable body or subsequent to collection. Advantageously, hydrogen recovered from the gas products can be reintroduced into the liquid product for upgrading. Regardless, hydrotreating or hydrodesulfurization can be very useful in reducing nitrogen and sulfur content in final hydrocarbon products. Optionally, catalysts can be introduced to facilitate such reactions. In addition, introduction of light hydrocarbons into the permeable body can result in reforming reactions which reduce the molecular weight, while increasing the hydrogen to carbon ratio. This is particularly advantageous due at least in part to high permeability of the permeable body, e.g. often around 30%-40% void volume although void volume can generally vary from about 10% to about 50% void volume. Light hydrocarbons which can be injected can be any which provide reforming to recovered hydrocarbons. Non-limiting examples of suitable light hydrocarbons include natural gas, natural gas condensates, industrial solvents, hydrogen donor agents, and other hydrocarbons having ten or fewer carbons, and often five or fewer carbons. Currently, natural gas is an effective, convenient and plentiful light hydrocarbon. As mentioned previously, various solvents or other additives can also be added to aid in extraction of hydrocarbon products from the oil shale and can often also increase fluidity.\|[0084] The light hydrocarbon can be introduced into the permeable body by conveying the same through a delivery conduit having an open end in fluid communication with a lower portion of the permeable body such that the light hydrocarbons (which are a gas under normal operating conditions) permeate up through the permeable body. Alternatively, this same approach can be applied to recovered hydrocarbons which are first delivered to an empty impoundment. In this way, the impoundment can act as a holding tank for direct products from a nearby impoundment and as a reformer or upgrader. In this embodiment, the impoundment can be at least partially filled with a liquid product where the gaseous light hydrocarbon is passed through and allowed to contact the liquid hydrocarbon products at temperatures and conditions sufficient to achieve reforming in accordance with well known processes. Optional reforming catalysts which include metals such as Pd, Ni or other suitable catalytically active metals can also be included in the liquid product within the impoundment. The addition of catalysts can serve to lower and/or adjust reforming temperature and/or pressure for particular liquid products. Further, the impoundments can be readily formed at almost any depth. Thus, optimal reforming pressures (or recovery pressures when using impoundment depth as pressure control measure for recovery from a permeable body) can be designed based on hydrostatic pressure due to the amount of liquid in the impoundment and the height of the impoundment, i.e. P=ρgh. In addition, the pressure can vary considerably over the height of the impoundment sufficient to provide multiple reforming zones and tailorable pressures. Generally, pressures within the permeable body can be sufficient to achieve substantially only liquid extraction, although some minor volumes of vapor may be produced depending on the particular composition of the permeable body. As a general guideline, pressures can range from about 5 atm to about 50 atm, although pressures from about 6 atm to about 20 atm can be particularly useful. However, any pressure greater than about atmospheric can be used.\|[0085] In certain instances the maintaining of a positive pressure within the enclosed capsule, relative to the outside atmosphere, has certain advantages. For example, a positive pressure prevents unwanted gases from entering into the impoundment during the hydrocarbon removal process and further expedites the removal of hydrocarbons from within the impoundment. Maintaining a positive pressure by means of a non-oxidizing gas reduces the likelihood of unwanted combustion and retards or prevents polymerization of lighter hydrocarbons which can form deposits on pipes or other infrastructure within the impoundment. Also, a positive pressure enables the flushing of the system in the event of certain events or happenings. One example might be in the event there is an interruption of the processing of the hydrocarbonaceous material and the collection of hydrocarbons due to a leak or other unwanted escape of fluids from within the impoundment. A positive pressure allows for the almost instantaneous introduction of non-oxidizing gases at a predetermined temperature, preferably a cooling temperature, to flush hydrocarbons and other vaporous components from the permeable body and within the impoundment so as to maintain an inert environment until any problem is detected and corrected. As previously noted gases such as hydrogen, nitrogen, propane, carbon dioxide, hydrocarbons, and the like can be used to flush the impoundment. Although any functional positive pressure can be suitable, pressure can generally be from about 1.01 atm to about 10 atm, and in one aspect from about 1.1 atm to about 4 atm.\|[0086] Further, once the hydrocarbon production stage is completed, the impoundment can be flushed with a non-oxidizing gas in order to remove further recoverable hydrocarbons from the impoundment. Such flushing can be accomplished in stages or in increments of temperature reduction or any other means to recover meaningful quantities of hydrocarbons. It may be beneficial to allow such flushing and cooling in increments such as to maximize the recovery of hydrocarbons while, at the same time, prepare the hydrocarbon lean shale or other materials, for further processing and/or pacification. The flushing times will obviously depend on the size of the permeable body and the impoundment and can be accomplished in a matter of hours, days or even weeks.\|[0087] Also, the lean shale or other inorganic matter resulting from the termination of the hydrocarbon removal process may still contain other components such as heavy metals, precious metals or other mineral components in the permeable body that can be extracted in further processing steps. Certain deposits may contain radioactive materials that require further processing and/or impounding in order to comply with governmental regulations.\|[0088] In one embodiment, extracted crude has fines precipitated out within the subdivided capsules. Extracted fluids and gases can be treated for the removal of fines and dust particles. Separation of fines from shale oil can be accomplished by techniques such as, but not limited to, hot gas filtering, precipitation, and heavy oil recycling.\|[0089] Hydrocarbon products recovered from the permeable body can be further processed (e.g. refined) or used as produced. Any condensable gaseous products can be condensed by cooling and collection, while non-condensable gases can be collected, burned as fuel, reinjected, or otherwise utilized or disposed of Optionally, mobile equipment can be used to collect gases. These units can be readily oriented proximate to the control infrastructure and the gaseous product directed thereto via suitable conduits from an upper region of the control infrastructure.\|[0090] In yet another alternative embodiment, heat within the permeable body can be recovered subsequent to primary recovery of hydrocarbon materials therefrom. For example, a large amount of heat is retained in the permeable body. In one optional embodiment, the permeable body can be flooded with a heat transfer fluid such as water to form a heated fluid, e.g. heated water and/or steam. At the same time, this process can facilitate removal of some residual hydrocarbon products via a physical rinsing of the spent shale solids. In some cases, the introduction of water and presence of steam can result in water gas shift reactions and formation of synthesis gas. Steam recovered from this process can be used to drive a generator, directed to another nearby infrastructure, or otherwise used. Hydrocarbons and/or synthesis gas can be separated from the steam or heated fluid by conventional methods.\|[0091] Although the methods and infrastructure allow for improved permeability and control of operating conditions, significant quantities of unrecovered hydrocarbons, precious metals, minerals, sodium bicarbonate or other commercially valuable materials often remain in the permeable body. Therefore, a selective solvent can be injected or introduced into the permeable body. Typically, this can be done subsequent to collecting the hydrocarbons, although certain selective solvents can be beneficially used prior to heating and/or collection. This can be done using one or more of the existing conduits or by direct injection and percolation through the permeable body. The selective solvent or leachate can be chosen as a solvent for one or more target materials, e.g. minerals, precious metal, heavy metals, hydrocarbons, or sodium bicarbonate. In one specific embodiment, steam or carbon dioxide can be used as a rinse of the permeable body to dislodge at least a portion of any remaining hydrocarbons. This can be beneficial not only in removing potentially valuable secondary products, but also in cleaning remaining spent materials of trace heavy metal or inorganics to below detectable levels in order to comply with regulatory standards or to prevent inadvertent leaching of materials at a future date.\|[0092] More particularly, various recovery steps can be used either before or after heating of the permeable body to recover heavy metals, precious metals, trace metals or other materials which either have economic value or may cause undesirable problems during heating of the permeable body. Typically, such recovery of materials can be performed prior to heat treatment of the permeable body. Recovery steps can include, but are in no way limited to, solution mining, leaching, solvent recovery, precipitation, acids (e.g. hydrochloric, acidic halides, etc.), flotation, ionic resin exchange, electroplating, or the like. For example, heavy metals, bauxite or aluminum, and mercury can be removed by flooding the permeable body with an appropriate solvent and recirculating the resulting leachate through appropriately designed ion exchange resins (e.g. beads, membranes, etc.).\|[0093] Similarly, bioextraction, bio leaching, biorecovery, or bioremediation of hydrocarbon material, spent materials, or precious metals can be performed to further improve remediation, extract valuable metals, and restoration of spent material to environmentally acceptable standards. In such bioextraction scenarios, conduits can be used to inject catalyzing gases as a precursor which helps to encourage bioreaction and growth. Such microorganisms and enzymes can biochemically oxidize the ore body or material or cellulosic or other biomass material prior to an ore solvent extraction via bio-oxidation. For example, a perforated pipe or other mechanism can be used to inject a light hydrocarbon (e.g. methane, ethane, propane or butane) into the permeable body sufficient to stimulate growth and action of native bacteria. Bacteria can be native or introduced and may grow under aerobic or anaerobic conditions. Such bacteria can release metals from the permeable body which can then be recovered via flushing with a suitable solvent or other suitable recovery methods. The recovered metals can then be precipitated out using conventional methods.\|[0094] Synthesis gas can also be recovered from the permeable body during the step of heating. Various stages of gas production can be manipulated through processes which raise or lower operating temperatures within the encapsulated volume and adjust other inputs into the impoundment to produce synthetic gases which can include but are not limited to, carbon monoxide, hydrogen, hydrogen sulfide, hydrocarbons, ammonia, water, nitrogen or various combinations thereof. In one embodiment, temperature and pressure can be controlled within the permeable body to lower CO2 emissions as synthetic gases are extracted.\|[0095] Hydrocarbon product recovered from the constructed infrastructures can most often be further processed, e.g. by upgrading, refining, etc. Sulfur from related upgrading and refining processing can be isolated in various constructed sulfur capsules within the greater structured impoundment capsule. Constructed sulfur capsules can be spent constructed infrastructures or dedicated for the purpose of storage and isolation after desulfurization.\|[0096] Similarly, spent hydrocarbonaceous material remaining in the constructed infrastructure can be utilized in the production of cement and aggregate products for use in construction or stabilization of the infrastructure itself or in the formation of offsite constructed infrastructures. Such cement products made with the spent shale may include, but are not limited to, mixtures with Portland cement, calcium salt, volcanic ash, perlite, synthetic nano carbons, sand, fiber glass, crushed glass, asphalt, tar, binding resins, cellulosic plant fibers, and the like.\|[0097] In still another embodiment, injection, monitoring and production conduits or extraction egresses can be incorporated into any pattern or placement within the constructed infrastructure. Monitoring wells and constructed geo membrane layers beneath or outside of the constructed capsule containment can be employed to monitor unwanted fluid and moisture migration outside of containment boundaries and the constructed infrastructure.\|[0098] Although a filled and prepared constructed infrastructure can often be immediately heated to recover hydrocarbons, this is not required. For example, a constructed infrastructure which is built and filled with mined hydro carbonaceous material can be left in place as a proven reserve. Such structures are less susceptible to explosion or damage due to terrorist activity and can also provide strategic reserves of unprocessed petroleum products, with classified and known properties so that economic valuations can be increased and more predictable. Long term petroleum storage often faces quality deterioration issues over time. Thus, these approaches can optionally be used for long term quality insurance and storage with reduced concerns regarding breakdown and degradation of hydrocarbon products.\|[0099] In still another aspect, the high quality liquid product can be blended with more viscous lower quality (e.g. lower API) hydrocarbon products. For example, kerogen oil produced from the impoundments can be blended with bitumen to form a blended oil. The bitumen is typically not transportable through an extended pipeline under conventional and accepted pipeline standards and can have a viscosity substantially above and an API substantially below that of the kerogen oil. By blending the kerogen oil and bitumen, the blended oil can be rendered transportable without the use of additional diluents or other viscosity or API modifiers. As a result, the blended oil can be pumped through a pipeline without requiring additional treatments to remove a diluent or returning such diluents via a secondary pipeline. Conventionally, bitumen is combined with a diluent such as natural gas condensate or other low molecular weight liquids, to allow pumping to a remote location. The diluent is removed and returned via a second pipeline back to the bitumen source. These approaches allow for elimination of returning diluent and simultaneous upgrading of the bitumen.\|[0100] Although these processes are mining-dependent, they are not limited or encumbered to conventional aboveground (ex-situ) retorting processes. This approach improves upon the benefits of surface retorts including better process control of temperature, pressure, injection rates, fluid and gas compositions, product quality and better permeability due to processing and heating mined rubble. These advantages are available while still addressing the volume, handling, and scalability issues most fabricated surface retorts cannot provide.\|[0101] Other improvements which can be realized are related to environmental protection. Conventional surface retorts have had the problem of spent shale after it has been mined and has passed through a surface retort. Spent shale which has been thermally altered requires special handling to reclaim and isolate from surface drainage basins and underground aquifers. This approach addresses reclamation and retorting in a uniquely combined approach. In regards to air emissions which are also a major problem typical of prior surface retort methods, this approach, because of its enormous volume capacity and high permeability, can accommodate longer heating residence times and therefore lower temperatures. One benefit of lower temperatures in the extraction process is that carbon dioxide production from decomposition of carbonates in the oil shale ore can be substantially limited thereby dramatically reducing CO2 emissions and atmospheric pollutants. This approach uniquely provides solutions to problems for not just one, but many problems, and in an integrated approach. As a result, significant benefits to the public can be achieved in terms of energy production, economic opportunity, environmental stewardship and energy output.\|[0102] It is to be understood that the above-referenced arrangements are illustrative of the application for the principles of the present invention. Thus, while the present invention has been described above in connection with the exemplary embodiments, it will be apparent to those of ordinary skill in the art that numerous modifications and alternative arrangements can be made without departing from the principles and concepts of the invention as set forth in the claims.	Family Number\|(35292)\|35292\|Title\|(EA201171025 A1)\|Methods for recovering hydrocarbons from carbon dioxide capture material using constructed infrastructure and associated overpressure systems\|Advantages / Prev. Drawbacks\|(CN102395653B B)\|Other methods include in situ radio frequency methods ( microwaves ) and " modified " in situ processes where underground mining , blasting and retorting have been used in combination to produce crushed rock from a formation to allow for better heat transfer and product removal . \|(CN102395653 A)\|Other methods include in situ radio frequency methods ( microwaves ) and " modified " in situ processes where underground mining , blasting and retorting have been used in combination to produce crushed rock from a formation to allow for better heat transfer and product removal . \|	Basic materials chemistry\|Civil engineering\|Materials, metallurgy	C10B-047/02\|C10B-053/06\|C10G-001/02\|C10G-001/04		C10B-047/02\|C10B-053/06\|C10G-001/02\|C10G-001/04	C01G-009/00\|C10B-047/02\|C10B-053/06\|C10G\|C10G-001/02\|C10G-001/04\|C10G-009/00\|E21B\|E21B-043/00	C01G-009/00\|C10B-047/02\|C10B-053/06\|C10G\|C10G-001/00\|C10G-001/02\|C10G-001/04\|C10G-009/00\|C10G-031/00\|C10G-031/06\|E21B\|E21B-043/00	PCLO=208400000\|PCLX=299006000\|PCLX=299003000\|PCLX=052169800\|PCLX=405129270\|PCLX=405129570\|PCLX=405130000\|PCLX=405128350\|PCLX=405128650\|PCLX=405128550\|PCLX=405128850\|PCLX=405129850\|PCLX=405128400\|PCLX=299002000\|PCLX=299014000\|PCLX=405128600\|PCLX=405129700\|PCLX=405128900\|PCLX=405128800	PCLO=208400000 PCLX=299002000 PCLX=299003000 PCLX=299006000 PCLX=299014000 PCLX=405128350 PCLX=405128400 PCLX=405128550 PCLX=405128600 PCLX=405128650 PCLX=405128800 PCLX=405128850 PCLX=405128900 PCLX=405129270 PCLX=405129570 PCLX=405129700 PCLX=405129850 PCLX=405130000 PCLX=052169800\|PCLO=208390000 PCLX=208177000 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WHO=Examiner SELF=Y\|US20080190815 1861751 WHO=Third_party SELF=Y\|US20080190816 1861751 WHO=Examiner SELF=Y\|US20080190816 1861751 WHO=Third_party SELF=Y\|US20080190818 1861751 WHO=Examiner SELF=Y\|US20080190818 1861751 WHO=Third_party SELF=Y\|US7862705 1861751 WHO=Third_party SELF=Y\|US7862706 43740497 WHO=Examiner SELF=Y\|US7862706 43740497 WHO=Third_party SELF=Y\|WO200898177 1861751 WHO=Third_party SELF=Y\|WO200898177 1861751 WHO=Examiner SELF=Y\|WO200898177 1861751 WHO=Examiner SELF=Y\|US20090190815 14923308 WHO=Examiner SELF=N\|US20060213657 1632664 WHO=Examiner SELF=N\|US20060213657 1632664 WHO=Third_party SELF=N\|JP2005306721 32305683 WHO=Third_party SELF=N\|US20070023186 1767434 WHO=Examiner SELF=N\|US20070023186 1767434 WHO=Third_party SELF=N\|US7121342 1761158 WHO=Third_party SELF=N\|US20070000662 61974990 WHO=Examiner SELF=N\|US20070000662 61974990 WHO=Third_party SELF=N\|US7091460 1781771 WHO=Examiner SELF=N\|US7091460 1781771 WHO=Third_party SELF=N\|US7073578 60130161 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43481366 WHO=Applicant SELF=N\|US7090013 88621749 WHO=Examiner SELF=N\|US7090013 88621749 WHO=Applicant SELF=N\|US7114566 88621749 WHO=Third_party SELF=N\|US6929330 1438851 WHO=Examiner SELF=N\|US6929330 1438851 WHO=Applicant SELF=N\|US6875356 43410084 WHO=Examiner SELF=N\|US6875356 43410084 WHO=Applicant SELF=N\|US6854328 43406177 WHO=Examiner SELF=N\|US6918443 1632664 WHO=Examiner SELF=N\|US6918443 1632664 WHO=Applicant SELF=N\|US6923257 1632664 WHO=Examiner SELF=N\|US6923257 1632664 WHO=Applicant SELF=N\|US6951247 1632664 WHO=Applicant SELF=N\|US6991033 1632664 WHO=Examiner SELF=N\|US6991033 1632664 WHO=Applicant SELF=N\|US7004247 1632664 WHO=Examiner SELF=N\|US7004247 1632664 WHO=Applicant SELF=N\|US7004251 1632664 WHO=Examiner SELF=N\|US7004251 1632664 WHO=Applicant SELF=N\|US7032660 1632664 WHO=Examiner SELF=N\|US7032660 1632664 WHO=Applicant SELF=N\|US7040397 1632664 WHO=Examiner SELF=N\|US7040397 1632664 WHO=Applicant SELF=N\|US7040399 1632664 WHO=Examiner SELF=N\|US7040399 1632664 WHO=Applicant SELF=N\|US7051811 1632664 WHO=Examiner SELF=N\|US7051811 1632664 WHO=Applicant SELF=N\|CN1432097 106759985 WHO=Examiner SELF=N\|US6732796 68371357 WHO=Examiner SELF=N\|US6732796 68371357 WHO=Applicant SELF=N\|US6632047 713363 WHO=Applicant SELF=N\|US6811683 48134 WHO=Applicant SELF=N\|US6543535 1439019 WHO=Examiner SELF=N\|US6543535 1439019 WHO=Applicant SELF=N\|US6543539 43300513 WHO=Examiner SELF=N\|US6543539 43300513 WHO=Applicant SELF=N\|US6485232 43276119 WHO=Applicant SELF=N\|US6824328 43394739 WHO=Applicant SELF=N\|US6419423 43252358 WHO=Examiner SELF=N\|US6419423 43252358 WHO=Applicant SELF=N\|US5997214 603718 WHO=Applicant SELF=N\|US6051137 42943979 WHO=Examiner SELF=N\|US6051137 42943979 WHO=Applicant SELF=N\|US6102622 1555459 WHO=Examiner SELF=N\|US6102622 1555459 WHO=Applicant SELF=N\|US5948253 43082999 WHO=Examiner SELF=N\|US5948253 43082999 WHO=Applicant SELF=N\|US5868202 1579437 WHO=Examiner SELF=N\|US5868202 1579437 WHO=Applicant SELF=N\|US5843214 43045633 WHO=Applicant SELF=N\|US6110359 43143044 WHO=Examiner SELF=N\|US6110359 43143044 WHO=Applicant SELF=N\|US5660500 42961429 WHO=Examiner SELF=N\|US5660500 42961429 WHO=Applicant SELF=N\|US5656239 42964545 WHO=Examiner SELF=N\|US5656239 42964545 WHO=Applicant SELF=N\|US5674424 42972644 WHO=Examiner SELF=N\|US5674424 42972644 WHO=Applicant SELF=N\|US5553189 42908634 WHO=Examiner SELF=N\|US5553189 42908634 WHO=Applicant SELF=N\|US5543041 13985117 WHO=Examiner SELF=N\|US5543041 13985117 WHO=Applicant SELF=N\|US5372621 42836640 WHO=Applicant SELF=N\|US5478443 13970508 WHO=Applicant SELF=N\|US5318116 42754267 WHO=Examiner SELF=N\|US5318116 42754267 WHO=Applicant SELF=N\|US5372708 2640335 WHO=Applicant SELF=N\|US5271693 42785257 WHO=Applicant SELF=N\|US5229583 42780625 WHO=Examiner SELF=N\|US5229583 42780625 WHO=Applicant SELF=N\|US5221827 42764654 WHO=Examiner SELF=N\|US5221827 42764654 WHO=Applicant SELF=N\|US5340467 42820083 WHO=Examiner SELF=N\|US5340467 42820083 WHO=Applicant 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SELF=N\|US4158622 60009376 WHO=Examiner SELF=N\|US4158622 60009376 WHO=Applicant SELF=N\|US4171146 42406771 WHO=Applicant SELF=N\|US4219237 42418416 WHO=Examiner SELF=N\|US4219237 42418416 WHO=Applicant SELF=N\|US4423907 42496584 WHO=Examiner SELF=N\|US4423907 42496584 WHO=Applicant SELF=N\|US4106814 60000211 WHO=Examiner SELF=N\|US4106814 60000211 WHO=Applicant SELF=N\|US4133580 42380326 WHO=Examiner SELF=N\|US4133580 42380326 WHO=Applicant SELF=N\|US4096912 42373399 WHO=Examiner SELF=N\|US4096912 42373399 WHO=Applicant SELF=N\|US4266612 3764056 WHO=Examiner SELF=N\|US4266612 3764056 WHO=Applicant SELF=N\|US4155967 42388873 WHO=Examiner SELF=N\|US4266826 42354154 WHO=Examiner SELF=N\|US4266826 42354154 WHO=Applicant SELF=N\|US4017119 42326543 WHO=Examiner SELF=N\|US4017119 42326543 WHO=Applicant SELF=N\|US3954140 42302067 WHO=Examiner SELF=N\|US3954140 42302067 WHO=Applicant SELF=N\|US4043595 42354154 WHO=Examiner SELF=N\|US4043595 42354154 WHO=Applicant SELF=N\|US4043595 42354154 WHO=Examiner SELF=N\|US4029571 1586018 WHO=Examiner SELF=N\|US4029571 1586018 WHO=Applicant SELF=N\|US3919390 42279675 WHO=Applicant SELF=N\|US3910834 3700427 WHO=Examiner SELF=N\|US3910834 3700427 WHO=Applicant SELF=N\|US3661423 2484420 WHO=Examiner SELF=N\|US3661423 2484420 WHO=Applicant SELF=N\|US3652447 42118345 WHO=Examiner SELF=N\|US3652447 42118345 WHO=Applicant SELF=N\|US3617471 95008668 WHO=Applicant SELF=N\|US2481051 41253434 WHO=Examiner SELF=N\|US2481051 41253434 WHO=Applicant SELF=N\|US1919636 40761806 WHO=Examiner SELF=N\|US1919636 40761806 WHO=Applicant SELF=N		\|WO200898177; US20080190813; US4294563; US4043595\|\|\|\|\|\|\|\|WO200898177; US20090190815; US4043595; CN1432097; US4294563; WO2008098177\|WO200898177; US20080190813; US4294563; US4043595; US4449586; WO200906687\|\|\|WO200898177; WO2008098177\|\|\|\|\|\|US4151068; US4155967; US4376107; US4449586; US20080077430; US20090007484; US4133580; US4423907; US4424021; US4717146; US4984594; US6841077; US6991033; US20070000662; US7862705; US7862706; US4430195; US5868202; US6854328; US6854929; US7004247; US7004251; US7004678; US20070023186; US3652447; US4502920; US5190405; US5193934; US4017119; US4199327; US4440446; US6051137; US6543535; US6543539; US6875356; US6881009; US7032660; US3661423; US3954140; US4266612; US4266826; US5114497; US6732796; US7040397; US7040399; US7048051; US7051811; US7534926; US4029571; US4096912; US4158622; US4452689; US4454915; US5024487; US5221827; US5318116; US6902138; US7066254; US20110138649; US1919636; US4851134; US5229583; US6419423; US6918443; US7070758; US7073578; US7077198; US7077199; US20090190813; US4043595; US4106814; US4219237; US5041209; US5137539; US5139535; US5340467; US5543041; US5656239; US5660500; US6102622; US6110359; US6923257; US6929330; US7090013; US7091460; US20080190815; US20080190816; US20080190818; US2481051; US4221648; US5244310; US5553189; US5948253; US20060213657; US3910834; US4294563; US4353418; US5674424; US1919636; US2481051; US3617471; US3652447; US3661423; US3910834; US3919390; US3954140; US4017119; US4029571; US4043595; US4096912; US4106814; US4133580; US4158622; US4171146; US4199327; US4219237; US4221648; US4234230; US4241952; US4266612; US4266826; US4294563; US4303533; US4353418; US4415365; US4423907; US4424021; US4430195; US4440446; US4452689; US4454915; US4502920; US4851134; US4879019; US4984594; US5024487; US5041209; US5076727; US5114497; US5137539; US5139535; US5190405; US5193934; US5221827; US5229583; US5244310; US5271693; US5318116; US5340467; US5372621; US5372708; US5478443; US5543041; US5553189; US5656239; US5660500; US5674424; US5843214; US5868202; US5948253; US5997214; US6051137; US6102622; US6110359; US6419423; US6485232; US6543535; US6543539; US6632047; US6732796; US6811683; US6824328; US6841077; US6854929; US6875356; US6881009; US6902138; US6918443; US6923257; US6929330; US6951247; US6962466; US6991033; US7004247; US7004251; US7004678; US7032660; US7040397; US7040399; US7048051; US7051811; US7066254; US7070758; US7073578; US7077198; US7077199; US7090013; US7091460; US7114566; US7121342; US7534926; US7862705; US7862706; KR10-0595792; JP2005306721; US20040211569; US20060213657; US20070000662; US20070023186; US20080190813; US20080190815; US20080190816; US20080190818; US20090250380; US20100200467; US20110138649; WO200898177	(EP2406351)\|Search Report references [Examiner]\|-See also references of WO 2010093777A2\|\|(US8349171)\|Applicant references\|-US Application PCT/US2010/023874; filed Feb. 11, 2010; Todd Dana; ISR mailed Oct. 13, 2010.\|-Alternative Methods for Fluid Delivery and Recovery; Manual; Sep. 1994; United States Environmental Protection Agency; 87 pgs.\|-U.S. Appl. No. 12/703,638, filed Feb. 10, 2010, Todd Dana.\|-U.S. Appl. No. 12/704,440, filed Feb. 11, 2010, Todd Dana.\|-U.S. Appl. No. 12/702,899, filed Feb. 9, 2010, Todd Dana.\|-U.S. Appl. No. 12/704,596, filed Feb. 12, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,073, filed Feb. 5, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,141, filed Feb. 5, 2010, Todd Dana.\|-U.S. Appl. No. 12/701,156, filed Feb. 5, 2010, Todd Dana.\|-Slow Sand Filter: http://en.wikipedia.org/wiki/Slow-sand-filter; Nov. 9, 2009; 4 pages.\|-Sand Filter: http://en.wikipedia.org/wiki/Sand-filter; Nov. 9, 2009; 6 pages.\|-Related Case: U.S. Appl. No. 12/960,215, filed Dec. 3, 2010; James Patten.\|-Related Case: U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana.\|-U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana; office action issued Jun. 1, 2011.\|-PCT Application PCT/US2010/058948; filed Dec. 13, 2010; James W. Patten; International Search Report mailed Aug. 31, 2011.\|-PCT Application PCT/US2010/060854; filed Dec. 16, 2010; James W. Patten; International Search Report mailed Aug. 26, 2011.\|-U.S. Appl. No. 12/984,394, filed Jan. 4, 2011; Todd Dana; Notice of Allowance issued Oct. 26, 2011.\|-U.S. Appl. No. 12/701,156, filed Feb. 5, 2010; Todd Dana; office action issued Mar. 12, 2012.\|-U.S. Appl. No. 12/701,156, filed Feb. 5, 2010; Todd Dana; notice of allowance dated Jul. 30, 2012.\|\|(WO2010/093777)\|International Search Report [Examiner]\|-See also references of EP 2406351A2\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|\|	GRANTED	(EP2406351)\|LAPSED\|(US8349171)\|LAPSED\|(WO2010/093777)\|LAPSED\|(CN102395653)\|LAPSED\|(VE2010000232)\|GRANTED\|(MY152426)\|GRANTED\|(MX320012)\|GRANTED\|(UA104617)\|GRANTED\|(EG26419)\|GRANTED\|(AU2010213774)\|EXPIRED\|(ZA201106555)\|GRANTED\|(MA33113)\|GRANTED\|(BRPI1008552)\|LAPSED\|(TN2011000392)\|PENDING\|(PE20120707)\|REVOKED\|(EA201171025)\|LAPSED\|(IN1891/MUMNP/2011)\|LAPSED\|(AP201105875)\|LAPSED\|(IL214550)\|LAPSED\|(CA2752133)\|LAPSED	ALIVE	(EP2406351)\|DEAD\|(US8349171)\|DEAD\|(WO2010/093777)\|DEAD\|(CN102395653)\|DEAD\|(VE2010000232)\|ALIVE\|(MY152426)\|ALIVE\|(MX320012)\|ALIVE\|(UA104617)\|ALIVE\|(EG26419)\|ALIVE\|(AU2010213774)\|DEAD\|(ZA201106555)\|ALIVE\|(MA33113)\|ALIVE\|(BRPI1008552)\|DEAD\|(TN2011000392)\|ALIVE\|(PE20120707)\|DEAD\|(EA201171025)\|DEAD\|(IN1891/MUMNP/2011)\|DEAD\|(AP201105875)\|DEAD\|(IL214550)\|DEAD\|(CA2752133)\|DEAD	(EP2406351)\|LEGAL DETAILS FOR EP2406351\|Actual or expected expiration date=2015-03-20\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP10741714\|Application date=2010-02-11\|Standardized application number=2010EP-0741714\|Event publication date=2011-12-16\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2012-01-18\|Event code=EP/A2\|Event group=Examination events\|Application published without search report\|Publication country=EP\|Publication number=EP2406351\|Publication stage code=A2\|Publication date=2012-01-18\|Standardized publication number=EP2406351\|Event publication date=2012-01-18\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2011-09-12\|Event publication date=2012-01-18\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR\|Event publication date=2012-05-16\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2014-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP2406351\|Publication stage code=A4\|Publication date=2014-09-17\|Standardized publication number=EP2406351\|Event publication date=2014-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2014-08-21\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2014-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2015-09-04\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2015-10-07\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2015-03-20\|(US8349171)\|LEGAL DETAILS FOR US8349171\|Actual or expected expiration date=2025-02-10\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-10\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US12703560\|Application date=2010-02-10\|Standardized application number=2010US-12703560\|Event publication date=2010-02-10\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:MCCAIG, BRIAN A\|Event publication date=2010-02-10\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1774\|Event publication date=2010-02-10\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 2488-019.NP\|Event publication date=2010-02-10\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 20551\|Event publication date=2010-02-10\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2010-02-10\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2010-03-01\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2010-03-01\|Event code=US/INCD\|Event group=Examination events OAO\|Notice Mailed--Application Incomplete--Filing Date Assigned\|Event publication date=2010-03-11\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DANA, TODD;PATTEN, JAMES W.;SIGNING DATES FROM 20090511 TO 20090623\|Reel/frame:024063/0749\|OWNER:RED LEAF RESOURCES, INC., UTAH\|Event publication date=2010-03-17\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|SECURITY AGREEMENT\|Assignors:RED LEAF RESOURCES, INC., DBA ECOSHALE AND ECOSHALE ENERGY;RED LEAF HOLDINGS, LLC;NATIONS MINING, LLC;AND OTHERS\|Reel/frame:024097/0397\|OWNER:CARDINAL ENERGY HOLDINGS, LLC, UTAH\|Effective date of the event=2009-07-02\|Event publication date=2010-04-12\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DANA, TODD;PATTEN, JAMES W.;SIGNING DATES FROM 20100317 TO 20100324\|Reel/frame:024215/0742\|OWNER:RED LEAF RESOURCES, INC., UTAH\|Event publication date=2010-04-29\|Event code=US/FLFEE\|Event group=Payment or non-payment notifications\|Payment of additional filing fee/Preexam\|Event publication date=2010-05-06\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2010-05-06\|Event code=US/POAC\|Event group=Change of name or address\|Change in Power of Attorney (May Include Associate POA)\|Event publication date=2010-05-10\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|RELEASE BY SECURED PARTY\|Assignor:CARDINAL ENERGY HOLDINGS, LLC.\|Reel/frame:024357/0626\|OWNER:RED LEAF RESOURCES, INC., D/B/A ECOSHALE, ECHOSHAL\|Effective date of the event=2010-05-07\|Event publication date=2010-05-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2010-08-12\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20100200467\|Publication stage code=A1\|Publication date=2010-08-12\|Standardized publication number=US20100200467\|Event publication date=2010-08-12\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2011-01-13\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-05-23\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2011-06-28\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-10-28\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2011-11-15\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2011-11-18\|Event code=US/DBLNF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection - Double Patenting\|RJD=2011-11-18\|R4R=DBL\|RJST=non-final\|Rejected claims 16\|RJCT=US7862705\|Event publication date=2011-11-18\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2011-11-18\|R4R=112\|RJST=non-final\|Rejected claims 1-2 and 9-11\|Event publication date=2011-11-18\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2011-11-18\|R4R=102b\|RJST=non-final\|Rejected claims 1-4 and 12; 1-5, 12-14, and 16\|RJCT=US4151068\|RJCT=US4449586\|Event publication date=2011-11-18\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2011-11-18\|R4R=102e\|RJST=non-final\|Rejected claims 1-2, 8, 12-13, and 15-16\|RJCT=US20090007484\|Event publication date=2011-11-18\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2011-11-18\|R4R=103a\|RJST=non-final\|Rejected claims 6 and 7\|RJCT=US4449586\|Event publication date=2011-12-14\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-02-21\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Action Recorded:\|RECD=2012-02-21\|Event publication date=2012-04-17\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Action Recorded:\|RECD=2012-04-17\|Event publication date=2012-04-19\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2012-04-24\|Event code=US/DBLNF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection - Double Patenting\|RJD=2012-04-24\|R4R=DBL\|RJST=non-final\|Rejected claims 16\|RJCT=US7862705\|Event publication date=2012-04-24\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2012-04-24\|R4R=102e\|RJST=non-final\|Rejected claims 16 and 17\|RJCT=US20080077430\|Event publication date=2012-04-24\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2012-04-24\|R4R=102b\|RJST=non-final\|Rejected claims 1, 3-4 and 12; 1, 3-5, 12-14, and 16\|RJCT=US4151068\|RJCT=US4449586\|Event publication date=2012-04-24\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2012-04-24\|R4R=103a\|RJST=non-final\|Rejected claims 6-8 and 15\|RJCT=US4449586\|Event publication date=2012-07-23\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-07-24\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2012-08-29\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2012-08-29\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2012-09-04\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2012-10-12\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2012-10-19\|Event code=US/M327\|Event group=Examination events OAO\|Miscellaneous Communication to Applicant - No Action Count\|Event publication date=2012-12-04\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2012-12-04\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2012-12-05\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2012-12-18\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2013-01-08\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US08349171\|Publication stage code=B2\|Publication date=2013-01-08\|Standardized publication number=US8349171\|Event publication date=2013-01-08\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 222 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 81 Adjustment total: \|Number of days of extension=141\|Event publication date=2016-01-19\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2016-06-15\|Event code=US/FPAY\|Event indicator=Pos\|Event group=Event indicating In Force Payment or non-payment notifications\|Fee payment recorded\|Annual fees payment date=2016-06-15\|Year of payment of annual fees=4\|Event publication date=2018-05-04\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2018-11-29\|Event code=US/M1559\|Event group=Payment or non-payment notifications\|Payment of Maintenance Fee under 1.28(c)\|Event publication date=2018-11-29\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2020-01-21\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|Event publication date=2020-05-01\|Event code=US/MAFP\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|Maintenance Fee Payment\|Annual fees payment date=2020-05-01\|Year of payment of annual fees=8\|PAYMENT OF MAINTENANCE FEE, 8TH YEAR, LARGE ENTITY (ORIGINAL EVENT CODE: M1552)\|Entity status of patent owner: LARGE ENTITY\|Event publication date=2020-05-01\|Event code=US/M1552\|Event group=Payment or non-payment notifications\|Payment of Maintenance Fee, 8th Year, Large Entity\|Event publication date=2024-01-23\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=11\|Event publication date=2024-08-26\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2025-01-08\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2025-01-08\|Event publication date=2025-02-10\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2025-02-10\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|(WO2010/093777)\|LEGAL DETAILS FOR WO2010/093777\|Actual or expected expiration date=2012-08-12\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOUS2010023874\|Application date=2010-02-11\|Standardized application number=2010WO-US23874\|Event publication date=2010-08-19\|Event code=WO/A2\|Event group=Examination events\|International application published with declaration under Article 17 (2) (a)\|Publication country=WO\|Publication number=WO2010093777\|Publication stage code=A2\|Publication date=2010-08-19\|Standardized publication number=WO201093777\|Event publication date=2010-12-09\|Event code=WO/A3\|Event indicator=Pos\|Event group=Examination events\|Later publication of ISR with revised front page\|Publication country=WO\|Publication number=WO2010093777\|Publication stage code=A3\|Publication date=2010-12-09\|Standardized publication number=WO201093777\|Event publication date=2012-08-12\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AP2011005875\|Actual or expected expiration date=2016-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=AP Corresponding appl: AP201105875\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2011AP-0005875\|Corresponding cc:\|Designated or member state=AP Corresponding pat: AP2011005875\|Publication stage code in the designated or member state=A0\|Publication date in the designated or member state=2011-10-31\|Publication number in the designated or member state=AP2011005875\|Event publication date=2011-10-31\|Event code=AP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=AP\|MEMBER STATE LEGAL DETAILS FOR AU2010213774\|Actual or expected expiration date=2016-09-08\|Legal state=DEAD\|Status=EXPIRED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2010213774\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010AU-0213774\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2010213774\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2011-09-22\|Publication number in the designated or member state=AU2010213774\|Event publication date=2011-08-31\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2011-09-22\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2016-09-08\|Event code=AU/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=AU\|MEMBER STATE LEGAL DETAILS FOR BRPI1008552\|Actual or expected expiration date=2016-09-13\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=BR Corresponding appl: BRPI1008552\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010BR-0008552\|Corresponding cc:\|Designated or member state=BR Corresponding pat: BRPI1008552\|Publication stage code in the designated or member state=A0\|Publication date in the designated or member state=2012-11-20\|Publication number in the designated or member state=BR201008552\|Event publication date=2012-11-20\|Event code=WO/REG\|Event code=BR/B01A\|Event group=Examination events\|Reference to a national code\|Pct publication - request for entry into the national phase\|Comunicacao da publicacao internacional pct. apresentacao de peticao de requerimento de entrada na fase nacional\|Corresponding cc:\|Designated or member state=BR\|Event publication date=2016-03-15\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2011-08-12\|Corresponding cc:\|Designated or member state=BR\|Event publication date=2017-01-10\|Event code=BR/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=BR\|MEMBER STATE LEGAL DETAILS FOR CA2752133\|Actual or expected expiration date=2016-02-11\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA2752133\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010CA-2752133\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA2752133\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2010-08-19\|Publication number in the designated or member state=CA2752133\|Event publication date=2011-08-10\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CA\|Event publication date=2016-03-24\|Event code=CA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR CL\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=CL Corresponding appl: CL2011001975\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CL\|MEMBER STATE LEGAL DETAILS FOR CN102395653\|Actual or expected expiration date=2016-02-11\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=CN Corresponding appl: CN201080016465\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010CN-80016465\|Corresponding cc:\|Designated or member state=CN Corresponding pat: CN102395653\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-03-28\|Publication number in the designated or member state=CN102395653\|Event publication date=2010-02-11\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CN\|Event publication date=2017-03-29\|Event code=CN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2011-08-12\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2011-08-12\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR DZ\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=DZ Corresponding appl: DZDZP2011000592\|Event publication date=2011-09-08\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=DZ\|MEMBER STATE LEGAL DETAILS FOR EA201171025\|Actual or expected expiration date=2017-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EA Corresponding appl: EA201171025\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2011EA-0071025\|Corresponding cc:\|Designated or member state=EA Corresponding pat: EA201171025\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2012-02-28\|Publication number in the designated or member state=EA201171025\|Event publication date=2011-09-08\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EA\|Event publication date=2012-02-28\|Event code=EA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EA\|MEMBER STATE LEGAL DETAILS FOR EG26419\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=EG Corresponding appl: EG2011081356\|Application date in the designated or member state=2011-08-11\|Application number in the designated or member state=2011EG-0081356\|Corresponding cc:\|Designated or member state=EG Corresponding pat: EG26419\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2013-10-23\|Publication number in the designated or member state=EG--26419\|Event publication date=2013-10-23\|Event code=EG/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EG\|MEMBER STATE LEGAL DETAILS FOR EP2406351\|Actual or expected expiration date=2015-03-20\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP10741714\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2010EP-0741714\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2406351\|Publication stage code in the designated or member state=A2\|Publication date in the designated or member state=2012-01-18\|Publication number in the designated or member state=EP2406351\|Event publication date=2010-10-06\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2011-09-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2015-10-07\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR GE\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=GE Corresponding appl: GE12376\|Event publication date=2011-09-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=GE\|MEMBER STATE LEGAL DETAILS FOR IL214550\|Actual or expected expiration date=2016-09-27\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IL Corresponding appl: IL214550\|Application date in the designated or member state=2011-02-11\|Application number in the designated or member state=2011IL-0214550\|Corresponding cc:\|Designated or member state=IL Corresponding pat: IL214550\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-09-27\|Publication number in the designated or member state=IL-214550\|Event publication date=2011-08-09\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IL\|Event publication date=2011-09-27\|Event code=IL/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IL\|MEMBER STATE LEGAL DETAILS FOR IN1891/MUMNP/2011\|Actual or expected expiration date=2022-02-03\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN1891/MUMNP/2011\|Application date in the designated or member state=2011-09-09\|Application number in the designated or member state=2011IN-MN01891\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN1891/MUMNP/2011\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2012-02-03\|Publication number in the designated or member state=IN2011MN01891\|Event publication date=2011-09-09\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|Event publication date=2012-02-03\|Event code=IN/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=IN\|MEMBER STATE LEGAL DETAILS FOR MA33113\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=MA Corresponding appl: MA34158\|Application date in the designated or member state=2011-09-09\|Application number in the designated or member state=2011MA-0034158\|Corresponding cc:\|Designated or member state=MA Corresponding pat: MA33113\|Publication stage code in the designated or member state=B1\|Publication date in the designated or member state=2012-03-01\|Publication number in the designated or member state=MA--33113\|Event publication date=2012-03-01\|Event code=MA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=MA\|MEMBER STATE LEGAL DETAILS FOR MX2011008534\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=MX Corresponding appl: MX2011008534\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2011MX-0008534\|Corresponding cc:\|Designated or member state=MX Corresponding pat: MX2011008534\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2011-12-16\|Publication number in the designated or member state=MX2011008534\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=MX\|Event publication date=2014-05-05\|Event code=MX/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=MX\|MEMBER STATE LEGAL DETAILS FOR PE\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=PE Corresponding appl: PE001479-2011\|Event publication date=2011-08-12\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=PE\|MEMBER STATE LEGAL DETAILS FOR TN2011000392\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=TN Corresponding appl: TN2011000392\|Application date in the designated or member state=2011-08-09\|Application number in the designated or member state=2011TN-0000392\|Corresponding cc:\|Designated or member state=TN Corresponding pat: TN2011000392\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2013-03-27\|Publication number in the designated or member state=TN2011000392\|MEMBER STATE LEGAL DETAILS FOR UA104617\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=UA Corresponding appl: UAA201110794\|Application date in the designated or member state=2010-02-11\|Application number in the designated or member state=2011UA-0010794\|Corresponding cc:\|Designated or member state=UA Corresponding pat: UA104617\|Publication stage code in the designated or member state=C2\|Publication date in the designated or member state=2014-02-25\|Publication number in the designated or member state=UA-104617\|Event publication date=2014-02-25\|Event code=UA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=UA\|MEMBER STATE LEGAL DETAILS FOR ZA201106555\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Corresponding cc:\|Designated or member state=ZA Corresponding appl: ZA201106555\|Application date in the designated or member state=2011-09-07\|Application number in the designated or member state=2011ZA-0006555\|Corresponding cc:\|Designated or member state=ZA Corresponding pat: ZA201106555\|Publication stage code in the designated or member state=B\|Publication date in the designated or member state=2012-05-30\|Publication number in the designated or member state=ZA201106555\|Event publication date=2012-05-30\|Event code=ZA/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=ZA\|(CN102395653)\|LEGAL DETAILS FOR CN102395653\|Actual or expected expiration date=2016-02-11\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201080016465\|Application date=2010-02-11\|Standardized application number=2010CN-80016465\|Event publication date=2012-03-28\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN102395653\|Publication stage code=A\|Publication date=2012-03-28\|Standardized publication number=CN102395653\|Event publication date=2012-03-28\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2012-05-09\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2015-05-06\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN102395653\|Publication stage code=B\|Publication date=2015-05-06\|Standardized publication number=CN102395653B\|Event publication date=2015-05-06\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2017-03-29\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee\|Effective date of the event=2016-02-11\|(VE2010000232)\|LEGAL DETAILS FOR VE2010000232\|Actual or expected expiration date=2030-02-12\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-12\|Event code=VE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=VE VE2010-000232\|Application date=2010-02-12\|Standardized application number=2010VE-0000232\|Event publication date=2012-07-26\|Event code=VE/A\|Event indicator=Pos\|Event group=Examination events\|Patent Application or Foreign Patent Application\|Publication country=VE\|Publication number=VE2010000232\|Publication stage code=A\|Publication date=2012-07-26\|Standardized publication number=VE2010000232\|Event publication date=2021-12-13\|Event code=VE/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted National or Foreign Invention Patent\|Publication country=VE\|Publication number=VE2010000232\|Publication stage code=B\|Publication date=2021-12-13\|Standardized publication number=VE2010000232\|(MY152426)\|LEGAL DETAILS FOR MY152426\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-11\|Event code=MY/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MY MYPI2011003744\|Application date=2010-02-11\|Standardized application number=2011MY-0003744\|Event publication date=2014-09-30\|Event code=MY/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent / Utility Model\|Publication country=MY\|Publication number=MY152426\|Publication stage code=A\|Publication date=2014-09-30\|Standardized publication number=MY-152426\|(MX320012)\|LEGAL DETAILS FOR MX320012\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-11\|Event code=MX/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MX MX2011008534\|Application date=2010-02-11\|Standardized application number=2011MX-0008534\|Event publication date=2011-12-16\|Event code=MX/A\|Event group=Examination events\|Patent application\|Publication country=MX\|Publication number=MX2011008534\|Publication stage code=A\|Publication date=2011-12-16\|Standardized publication number=MX2011008534\|Event publication date=2014-05-05\|Event code=MX/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent/ granted utility model\|Publication country=MX\|Publication number=MX320012\|Publication stage code=B\|Publication date=2014-05-05\|Standardized publication number=MX-320012\|Event publication date=2014-05-05\|Event code=MX/FG\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant or registration\|Concesion\|(UA104617)\|LEGAL DETAILS FOR UA104617\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2010-02-11\|Event code=UA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=UA UAA201110794\|Application date=2010-02-11\|Standardized application number=2011UA-0010794\|Event publication date=2014-02-25\|Event code=UA/C2\|Event indicator=Pos\|Event group=Event indicating In Force\|Pat. grant. upon the USSR appl.,for which no pos. dec. made;grant. upon basis of national application\|Publication country=UA\|Publication number=UA104617\|Publication stage code=C2\|Publication date=2014-02-25\|Standardized publication number=UA-104617\|(EG26419)\|LEGAL DETAILS FOR EG26419\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-08-11\|Event code=EG/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EG EG2011081356\|Application date=2011-08-11\|Standardized application number=2011EG-0081356\|Event publication date=2013-10-23\|Event code=EG/A\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent for invention / Patent of addition\|Publication country=EG\|Publication number=EG26419\|Publication stage code=A\|Publication date=2013-10-23\|Standardized publication number=EG--26419\|(AU2010213774)\|LEGAL DETAILS FOR AU2010213774\|Actual or expected expiration date=2016-09-08\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=2010-02-11\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2010213774\|Application date=2010-02-11\|Standardized application number=2010AU-0213774\|Event publication date=2011-09-22\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2010213774\|Publication stage code=A1\|Publication date=2011-09-22\|Standardized publication number=AU2010213774\|Event publication date=2013-06-13\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent proceeded by OPI\|Publication country=AU\|Publication number=AU2010213774\|Publication stage code=B2\|Publication date=2013-06-13\|Standardized publication number=AU2010213774\|Event publication date=2013-10-10\|Event code=AU/FGA\|Event indicator=Pos\|Event group=Event indicating In Force\|Letters patent sealed or granted (standard patent)\|Event publication date=2016-09-08\|Event code=AU/MK14\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent ceased section 143(a) (annual fees not paid) or expired\|(ZA201106555)\|LEGAL DETAILS FOR ZA201106555\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-09-07\|Event code=ZA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=ZA ZA201106555\|Application date=2011-09-07\|Standardized application number=2011ZA-0006555\|Event publication date=2012-05-30\|Event code=ZA/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=ZA\|Publication number=ZA201106555\|Publication stage code=B\|Publication date=2012-05-30\|Standardized publication number=ZA201106555\|(MA33113)\|LEGAL DETAILS FOR MA33113\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=GRANTED\|Event publication date=2011-09-09\|Event code=MA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MA MA34158\|Application date=2011-09-09\|Standardized application number=2011MA-0034158\|Event publication date=2012-03-01\|Event code=MA/B1\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted Patent\|Publication country=MA\|Publication number=MA33113\|Publication stage code=B1\|Publication date=2012-03-01\|Standardized publication number=MA--33113\|(BRPI1008552)\|LEGAL DETAILS FOR BRPI1008552\|Actual or expected expiration date=2016-09-13\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=BR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=BR BRPI1008552\|Application date=2010-02-11\|Standardized application number=2010BR-0008552\|Event publication date=2012-11-20\|Event code=BR/A0\|Event indicator=Pos\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=BR\|Publication number=BRPI1008552\|Publication stage code=A0\|Publication date=2012-11-20\|Standardized publication number=BR201008552\|Event publication date=2016-03-15\|Event code=BR/A2\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention / pipeline patent published without search report\|Publication country=BR\|Publication number=BRPI1008552\|Publication stage code=A2\|Publication date=2016-03-15\|Standardized publication number=BR201008552\|Event publication date=2016-09-13\|Event code=BR/B08F\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application fees: dismissal - article 86 of industrial property law\|Anuidade do pedido: arquivamento . Art. 86 da lpi [codigo 8.6 rpi]\|REFERENTE A 6A ANUIDADE.\|Event publication date=2017-01-10\|Event code=BR/B08K\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Lapse as no evidence of payment of the annual fee has been furnished to inpi (acc. art. 87)\|Manutencao do arquivamento [codigo 8.11 rpi]\|EM VIRTUDE DO ARQUIVAMENTO PUBLICADO NA RPI 2384 DE 13-09-2016 E CONSIDERANDO AUSENCIA DE MANIFESTACAO DENTRO DOS PRAZOS LEGAIS, INFORMO QUE CABE SER MANTIDO O ARQUIVAMENTO DO PEDIDO DE PATENTE, CONFORME O DISPOSTO NO ARTIGO 12, DA RESOLUCAO 113/2013.\|(TN2011000392)\|LEGAL DETAILS FOR TN2011000392\|Actual or expected expiration date=2030-02-11\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2011-08-09\|Event code=TN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=TN TN2011000392\|Application date=2011-08-09\|Standardized application number=2011TN-0000392\|Event publication date=2013-03-27\|Event code=TN/A1\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention\|Publication country=TN\|Publication number=TN2011000392\|Publication stage code=A1\|Publication date=2013-03-27\|Standardized publication number=TN2011000392\|(PE20120707)\|LEGAL DETAILS FOR PE20120707\|Actual or expected expiration date=2016-01-29\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2010-02-11\|Event code=PE/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=PE PE2011001479\|Application date=2010-02-11\|Standardized application number=2011PE-0001479\|Event publication date=2012-06-27\|Event code=PE/A1\|Event group=Examination events\|Patent application\|Publication country=PE\|Publication number=PE20120707\|Publication stage code=A1\|Publication date=2012-06-27\|Standardized publication number=PE201200707\|Event publication date=2016-01-29\|Event code=PE/FC\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Refusal\|Rechazada o denegada\|(EA201171025)\|LEGAL DETAILS FOR EA201171025\|Actual or expected expiration date=2017-02-28\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=EA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EA EA201171025\|Application date=2010-02-11\|Standardized application number=2011EA-0071025\|Event publication date=2012-02-28\|Event code=EA/A1\|Event group=Examination events\|Public. of applic. with search report\|Publication country=EA\|Publication number=EA201171025\|Publication stage code=A1\|Publication date=2012-02-28\|Standardized publication number=EA201171025\|Event publication date=2017-02-28\|Event code=EA/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IN1891/MUMNP/2011)\|LEGAL DETAILS FOR IN1891/MUMNP/2011\|Actual or expected expiration date=2022-02-03\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-09-09\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN1891/MUMNP/2011\|Application date=2011-09-09\|Standardized application number=2011IN-MN01891\|Event publication date=2012-02-03\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN1891/MUMNP/2011\|Publication stage code=A\|Publication date=2012-02-03\|Standardized publication number=IN2011MN01891\|Event publication date=2022-02-03\|Event code=IN/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(AP201105875)\|LEGAL DETAILS FOR AP201105875\|Actual or expected expiration date=2016-10-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=AP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AP AP201105875\|Application date=2010-02-11\|Standardized application number=2011AP-0005875\|Event publication date=2011-10-31\|Event code=AP/D0\|Event indicator=Pos\|Event group=Examination events\|Patent application filed\|Publication country=AP\|Publication number=AP201105875\|Publication stage code=D0\|Publication date=2011-10-31\|Standardized publication number=AP201105875\|Event publication date=2011-10-31\|Event code=AP/A0\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=AP\|Publication number=AP2011005875\|Publication stage code=A0\|Publication date=2011-10-31\|Standardized publication number=AP2011005875\|Event publication date=2016-10-31\|Event code=AP/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(IL214550)\|LEGAL DETAILS FOR IL214550\|Actual or expected expiration date=2016-09-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2011-02-11\|Event code=IL/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IL IL214550\|Application date=2011-02-11\|Standardized application number=2011IL-0214550\|Event publication date=2011-09-27\|Event code=IL/A\|Event group=Examination events\|Application of patent for invention\|Publication country=IL\|Publication number=IL214550\|Publication stage code=A\|Publication date=2011-09-27\|Standardized publication number=IL-214550\|Event publication date=2016-09-27\|Event code=IL/EEDL\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Pending application likely abandoned\|(CA2752133)\|LEGAL DETAILS FOR CA2752133\|Actual or expected expiration date=2016-02-11\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2010-02-11\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2752133\|Application date=2010-02-11\|Standardized application number=2010CA-2752133\|Event publication date=2010-08-19\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2752133\|Publication stage code=A1\|Publication date=2010-08-19\|Standardized publication number=CA2752133\|Event publication date=2016-03-24\|Event code=CA/FZDE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Dead\|Effective date of the event=2016-02-11	(EP2406351)\|Contracting States: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2010/093777)\|ARIPO: GH, GM, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2010/093777)\|EAPO: RU, TJ, BY, MD, AZ, TM, AM, KG, KZ\|(WO2010/093777)\|EPO: DE, NO, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2010/093777)\|OAPI: CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2010/093777)\|National States: PT, HN, HR, HU, ID, IL, AE, IN, AG, ZA, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, BH, JP, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KM, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PE, PG, PH, PL	(WO2010/093777)\|CL; DZ; EG; GE; MA; MX; PE; TN; UA; ZA\|(VE2010000232)\|VE\|(MY152426)\|MY\|(MX320012)\|MX\|(UA104617)\|UA\|(EG26419)\|EG\|(ZA201106555)\|ZA\|(MA33113)\|MA\|(TN2011000392)\|TN	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=jP3Nqvhw8TiycRSLnaM7OHmXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US8349171&ekey=948&xpn=EP2406351&kind=A4	https://register.epo.org/application?number=EP10741714	https://permalink.orbit.com/RenderStaticFirstPage?XPN=xq6OlXDbYJMuw56Xk6cpNXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(WO2010/093777)\|US\|(US8349171)\|US	(WO2010/093777)\|NAME=RED LEAF RESOURCES, INC. 200 W. Civic Center Drive, Suite 190, Sandy, UT 84070 , COUNTRY=US\|(US8349171)\|NAME=Red Leaf Resources, Inc. , CITY=Sandy , STATE=UT , COUNTRY=US , ATYP=US Company	(EP2406351)\|DE\|(EP2406351)\|DE\|\|(US20100200467)\|US\|(WO2010/093777)\|US\|\|\|\|\|\|\|(AU2010213774)\|AU\|(AU2010213774)\|AU\|(CA2752133)\|CA	(EP2406351)\|NAME=Walker, Ross Thomson;Forresters Skygarden Erika-Mann-Strasse 11 , CITY=80636 München , COUNTRY=DE , REG=101298687\|(EP2406351)\|NAME=Walker, Ross Thomson;Forrester & Boehmert Pettenkoferstrasse 20-22 , CITY=80336 München , COUNTRY=DE , REG=100045009\|(US8349171)\|NAME=Thorpe North & Western LLP\|(US20100200467)\|NAME=THORPE NORTH & WESTERN, LLP. P.O. Box 1219 , CITY=SANDY , STATE=UT , POSTCODE=84091-1219 , COUNTRY=US\|(WO2010/093777)\|NAME=Ericksen Erik S. et al. Thorpe North & Western, LLP, Po Box 1219, Sandy, UT 84091-1219 , COUNTRY=US\|(CN102395653)\|NAME=ZHAO RONGMIN;JEEKAI & PARTNERS , REG=11245\|(CN102395653)\|NAME=ZHAO RONGMIN;JEEKAI & PARTNERS , REG=11245\|(VE2010000232)\|NAME=LINARES ALLOCA MARLIN ENEIDA\|(VE2010000232)\|NAME=LINARES ALLOCA MARLIN ENEIDA\|(MX320012)\|NAME=MARIA ANGELICA PARDAVELL JUAREZ\|(MX2011008534)\|NAME=MARIA ANGELICA PARDAVELL JUAREZ\|(AU2010213774)\|NAME=FB Rice Level 23 44 Market Street , CITY=SYDNEY , STATE=NSW , POSTCODE=2000 , COUNTRY=AU\|(AU2010213774)\|NAME=FB Rice Level 23 44 Market Street , CITY=Sydney , STATE=NSW , POSTCODE=2000 , COUNTRY=AU\|(CA2752133)\|NAME=BERESKIN & PARR LLP/S.E.N.C.R.L.,S.R.L. , COUNTRY=CA	(EP2406351)\|US; US\|(EP2406351)\|US; US\|(US8349171)\|US; US\|(US20100200467)\|US; US\|\|(WO2010/093777)\|US; US\|\|\|\|\|(MX320012)\|US; US\|\|\|\|\|\|\|\|\|\|\|(IN1891/MUMNP/2011)\|US; US\|\|(CA2752133)\|US; US	(EP2406351)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, CITY=Park CityUT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., CITY=SandyUT 84092, COUNTRY=US\|(EP2406351)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, CITY=Park CityUT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., CITY=SandyUT 84092, COUNTRY=US\|(US8349171)\|NAME=Dana Todd, CITY=Park City, STATE=UT , COUNTRY=US \|NAME=Patten James W., CITY=Sandy, STATE=UT , COUNTRY=US\|(US20100200467)\|NAME=Dana Todd, CITY=Park City, STATE=UT , COUNTRY=US \|NAME=Patten James W., CITY=Sandy, STATE=UT , COUNTRY=US\|(WO2010/093777)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(WO2010/093777)\|NAME=DANA, Todd 3473 W. Daybreaker Drive, Park City, UT 84098, COUNTRY=US \|NAME=PATTEN, James, W. 4216 E. Wildcreek Rd., Sandy, UT 84092, COUNTRY=US\|(CN102395653)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(CN102395653)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(VE2010000232)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(MY152426)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES W.\|(MX320012)\|NAME=TODD DANA, COUNTRY=US \|NAME=JAMES W PATTEN, COUNTRY=US\|(MX2011008534)\|NAME=TODD DANA\|NAME=JAMES W PATTEN\|(UA104617)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(EG26419)\|NAME=DANA TODD 3473 W. Daybreaker Drive Park City, UT 84098-US)\|NAME=PATTEN JAMES W 4216 E. Wildcreek Rd. Sandy, UT 84092-US\|(AU2010213774)\|NAME=Dana, Todd\|NAME=Patten, James W.\|(AU2010213774)\|NAME=Dana, Todd\|NAME=Patten, James W.\|(ZA201106555)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(MA33113)\|NAME=DANA, TODD\|NAME=PATTEN, JAMES, W.\|(BRPI1008552)\|NAME=JAMES W. PATTEN 4216 E.WILDCREEK RD SANDY UT US - 84092 US\|NAME=TODD DANA 3473 W. DAYBREAKER DRIVE PARK CITY UT US-84098 US\|(TN2011000392)\|NAME=PATTEN JAMES W.\|NAME=DANA TODD\|(PE20120707)\|NAME=PATTEN, JAMES W.\|NAME=DANA, TODD\|(IN1891/MUMNP/2011)\|NAME=TODD DANA, COUNTRY=US \|NAME=PATTEN JAMES W, COUNTRY=US\|(AP2011005875)\|NAME=DANA TODD\|NAME=PATTEN JAMES W\|(CA2752133)\|NAME=DANA, TODD, COUNTRY=US \|NAME=PATTEN, JAMES W., COUNTRY=US	(IN1891/MUMNP/2011)\|5\|(CN102395653)\|5\|(AU2010213774)\|5\|(CA2752133)\|5\|(US8349171)\|5	3	20		CARDINAL ENERGY HOLDINGS; FROM 2009-07-02; TO 2010-05-07	(EP2406351)\|WO2010/093777\|(CN102395653)\|WO2010/093777\|(MX320012)\|WO2010/093777\|(UA104617)\|WO2010/093777\|(EG26419)\|WO2010/093777\|(AU2010213774)\|WO2010/093777\|(ZA201106555)\|WO2010/093777\|(MA33113)\|WO2010/093777\|(BRPI1008552)\|WO2010/093777\|(TN2011000392)\|WO2010/093777\|(EA201171025)\|WO2010/093777\|(IN1891/MUMNP/2011)\|WO2010/093777\|(AP201105875)\|WO2010/093777\|(IL214550)\|WO2010/093777\|(CA2752133)\|WO2010/093777		Primary examiner: Pardo Torre, J\|\|Primary examiner: Pardo Torre, J\|\|(US8349171)\|Number of Claims: NCL=17\|Number of Drawings: NDR=5\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1,16\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=141\|Primary examiner: McCaig Brian\|Art Unit.: ART =1774\|\|(US20100200467)\|Number of Claims: NCL=16\|Number of Drawings: NDR=5\|Number of Figures: NFG=6\|Independent Claim Number: ICL=1,16\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: McCaig Brian\|Art Unit.: ART =1774\|\|(WO2010/093777)\|Number of Claims: NCL=16\|Extended kind: EXTK=z\|\|(CN102395653)\|Number of Claims: NCL=18\|Gazette date: GAZDATE=2015-05-06\|Gazette number: GAZNUM=31-18\|Substantial examination effective date: 20120509 Examination duration: 35 months\|Number of Pages: NPAGES=25\|Primary examiner: Zhou Shuge\|Primary examiner: 周淑歌\|\|(CN102395653)\|Number of Claims: NCL=16\|Gazette date: GAZDATE=2012-03-28\|Gazette number: GAZNUM=28-13\|Substantial examination effective date: 20120509 Examination duration: 35 months\|Number of Pages: NPAGES=24\|Primary examiner: Zhou Shuge\|Primary examiner: 周淑歌\|\|(MX2011008534)\|Number of Claims: NCL=16\|Number of Pages: NPAGES=88\|\|(AU2010213774)\|Number of Claims: NCL=17\|\|(AU2010213774)\|Number of Claims: NCL=16\|\|(IN1891/MUMNP/2011)\|Number of Claims: NCL=16\|\|(AP2011005875)\|Gazette date: GAZDATE=2011-10-31\|\|(CA2752133)\|Number of Claims: NCL=16\|Number of Pages: NPAGES=45\|	(US8349171)\|Provisional Appl: US61/152,146 FDD=2009-02-12 [2009US-61152146]\|Previous publication: US20100200467 A1 2010-08-12 [US20100200467]	(EP2406351)\|ENGLISH (ENG)	(VE2010000232)\|Patent\|(BR201008552)\|Patent\|(CN102395653B)\|Patent\|(MY-152426)\|Patent\|(EP2406351)\|Patent\|(MX-320012)\|Patent\|(UA-104617)\|Patent\|(EG--26419)\|Patent\|(AU2010213774)\|Patent\|(TN2011000392)\|Patent\|(US8349171)\|Patent\|(BR201008552)\|Patent\|(VE2010000232)\|Patent\|(PE201200707)\|Patent\|(ZA201106555)\|Patent\|(CN102395653)\|Patent\|(MA--33113)\|Patent\|(EA201171025)\|Patent\|(IN2011MN01891)\|Patent\|(EP2406351)\|Patent\|(MX2011008534)\|Patent\|(AP2011005875)\|Patent\|(AP201105875)\|Patent\|(IL-214550)\|Patent\|(AU2010213774)\|Patent\|(WO201093777)\|Patent\|(CA2752133)\|Patent\|(WO201093777)\|Patent\|(US20100200467)\|Patent	Titre: (EP2406351)\|Methods of recovering hydrocarbons from hydrocarbonaceous material using a constructed infrastructure and associated systems maintained under positive pressure Résumé: (EP2406351)\|A method of recovering hydrocarbons from hydrocarbonaceous materials can include forming a constructed permeability control infrastructure (100). This constructed infrastructure (100) defines a substantially encapsulated volume. A comminuted hydrocarbonaceous material can be introduced into the control infrastructure to form a permeable body (120) of hydrocarbonaceous material. The permeable body (120) can be heated sufficient to remove hydrocarbons therefrom. During heating and removal of hydrocarbons and subsequent thereto a positive pressure can be maintained within the encapsulated volume by means of a non-oxidizing gas to expedite flushing of hydrocarbonaceous material, inhibit unwanted entry of oxygen into the encapsulated volume and remove recoverable hydrocarbons following the heating process.	45	Abstract	gpt-4o-mini	no	The article focuses on recovering hydrocarbons from hydrocarbonaceous materials and does not mention accelerated weathering, CO₂ capture, or related processes.
43	US63/203,814P\|US63/203,814\|US17/815,914\|WOIB2022/057088\|US18/302,702\|US18/673,248	US18/673,248\|US18/302,702\|WOIB2022/057088\|IN202417013808\|EP22848809\|JP2024505303\|BR112024001825\|AU2022318480\|CA3227505\|US17/815,914	US12545576\|EP4377258\|US20240308843\|JP2024528907\|US12006212\|EP4377258\|BR112024001825\|IN202417013808\|AU2022318480\|BR112024001825\|US20230271827\|US20230102312\|CA3227505\|WO2023/007466	104224295	US12545576 B2 2026-02-10 [US12545576]\|US20240308843 A1 2024-09-19 [US20240308843]\|US12006212 B2 2024-06-11 [US12006212]\|US20230271827 A1 2023-08-31 [US20230271827]\|WO2023/007466 A1 2023-02-02 [WO202307466]\|IN202417013808 A 2024-03-15 [IN202417013808]\|EP4377258 A4 2025-09-17 [EP4377258]\|EP4377258 A1 2024-06-05 [EP4377258]\|JP2024528907 A 2024-08-01 [JP2024528907]\|BR112024001825 A2 2024-04-24 [BR112024001825]\|BR112024001825 A0 2024-02-06 [BR112024001825]\|AU2022318480 A1 2024-02-22 [AU2022318480]\|CA3227505 A1 2023-02-02 [CA3227505]\|US20230102312 A1 2023-03-30 [US20230102312]	2021-07-30\|2022-07-28\|2022-07-29\|2023-04-18\|2024-05-23	2024-05-23\|2023-04-18\|2022-07-29\|2024-02-26\|2022-07-29\|2022-07-29\|2022-07-29\|2022-07-29\|2022-07-29\|2022-07-28	2026-02-10\|2025-09-17\|2024-09-19\|2024-08-01\|2024-06-11\|2024-06-05\|2024-04-24\|2024-03-15\|2024-02-22\|2024-02-06\|2023-08-31\|2023-03-30\|2023-02-02\|2023-02-02	\|(US12545576)\|2026-02-10\|(US12006212)\|2024-06-11\|\|\|\|\|\|\|	(EP4377258)\|2042-07-29\|(US12545576)\|2042-07-28\|(US12006212)\|2042-07-28\|(US20230102312)\|2023-06-09\|(WO2023/007466)\|2025-01-30\|(JP2024528907)\|2026-03-09\|(BR112024001825)\|2042-07-29\|(IN202417013808)\|2042-07-29\|(AU2022318480)\|2042-07-29\|(CA3227505)\|2042-07-29	(EP4377258)\|Systems and methods for generating hydrogen and magnetite from rock	(EP4377258)\|Systems and methods for sequestering carbon, evolving hydrogen gas, producing iron oxide as magnetite, and producing magnesium carbonate as magnesite through sequential carbonation and serpentinization/hydration reactions involving processed olivine- and/or pyroxene-rich ores, as typically found in mafic and ultramafic igneous rock. Precious or scarce metals, such nickel, cobalt, chromium, rare earth elements, and others, may be concentrated in the remaining ore to facilitate their recovery from any gangue material.	FOUNDATION OHIO STATE INNOVATION\|OHIO STATE INNOVATION FOUNDATION	(EP4377258)\|Ohio State Innovation Foundation\|(EP4377258)\|Ohio State Innovation Foundation ([US])\|(US12545576)\|Ohio State Innovation Foundation ([US])\|(US20240308843)\|Ohio State Innovation Foundation ([US])\|(US12006212)\|Ohio State Innovation Foundation ([US])\|(US20230271827)\|Ohio State Innovation Foundation ([US])\|(US20230102312)\|Ohio State Innovation Foundation ([US])\|(WO2023/007466)\|OHIO STATE INNOVATION FOUNDATION ([US])\|(JP2024528907)\|OHIO STATE INNOVATION FOUNDATION\|(BR112024001825)\|FOUNDATION OHIO STATE INNOVATION ([US])\|\|(IN202417013808)\|OHIO STATE INNOVATION FOUNDATION\|(AU2022318480)\|OHIO STATE INNOVATION FOUNDATION\|(CA3227505)\|OHIO STATE INNOVATION FOUNDATION ([US])	DARRAH THOMAS\|RAO VIKRAM\|WHYTE COLIN	(EP4377258)\|DARRAH, Thomas\|RAO, Vikram\|WHYTE, Colin\|(EP4377258)\|DARRAH, Thomas\|RAO, Vikram\|WHYTE, Colin	(EP4377258)\|K&L Gates LLP;Karolinen Karree ([DE])\|Reg. Nb: 101744768\|(US12545576)\|K&L Gates LLP\|(US12006212)\|K&L Gates LLP\|(WO2023/007466)\|EASWARAN, David ([US])\|(JP2024528907)\|KIMURA, Mitsuru\|Reg. Nb: 100095407\|Yasushi Morikawa\|Reg. Nb: 100132883\|Kei Sakurada\|Reg. Nb: 100148633\|Hide Mie\|Reg. Nb: 100147924\|(AU2022318480)\|K&L Gates ([AU])\|(CA3227505)\|ROWAND LLP ([CA])	(US12545576)\|It will be appreciated that the scope of the present disclosure encompasses many potential embodiments in addition to those summarized above, some of which will be described in further detail below.\|Conversely, hydrogen formation in a more conventional manner, such as by natural gas reforming, is limited by natural gas availability, among other constraints that are often carbon intensive.\|Instead, natural systems, which evolve through time and under varying reaction conditions produce complex (and often heterogeneous) complexes of varying mineral assemblages and products of reactions that did not follow the idealized reactions described above, or are slower to reach thermodynamic equilibrium.\|Such reactions produce variable and complex mineralogy and chemistry but do not predictably produce any specific combination of reaction products.\|	(US12545576)\|1. A system for sequestering carbon and producing hydrogen and magnetite from rock, the system comprising: a source of ore containing olivine or pyroxene; a reactor having an inlet that receives ore particles and at least one outlet, the reactor also having at least one additional inlet through which one or more of carbon dioxide or water is introduced, the reactor operable at a first temperature for a first residence time to react carbon dioxide that enters the reactor through the at least one additional inlet with the ore particles to generate magnesium carbonate, the reactor also operable at a second temperature for a second residence time to react water that enters the reactor through the at least one additional inlet with the ore particles to generate magnetite and hydrogen gas; and a gas separator that is connected to and in fluid communication with the at least one outlet of the reactor, the gas separator configured to separate hydrogen gas from gases that exit the reactor through the at least one outlet.\|18. A method for generating hydrogen and magnetite from rock, the method comprising: obtaining an ore containing olivine or pyroxene; introducing the ore into a reactor that is operable at temperatures above ambient temperature and pressures above atmospheric pressure; introducing water into the reactor at a particular temperature for a particular residence time to react with the ore to generate magnetite and hydrogen gas; removing, from the reactor, a gas mixture that includes the hydrogen gas; separating the hydrogen gas from the gas mixture; and removing any remaining ore from the reactor.\|	(US12545576)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|The disclosure herein provides one or more embodiments of systems and methods for sequestering carbon, evolving hydrogen gas, and producing magnetite as well as magnesite from olivine- and pyroxene-bearing ores.\|The disclosure herein provides one or more embodiments of systems and methods that facilitate the production of hydrogen, magnetite, and/or other desired minerals through serpentinization reactions involving olivine- and pyroxene-rich ores generally found in mafic and/or ultramafic igneous rock, or of any other rock assemblages containing such olivine- and pyroxene-rich ores.\|	(US12545576)\|MAGNETITE(100,58)\|ROCK(100,32)\|ORE PARTICLE(100,12)\|HYDROGEN GENERATION(100,6)\|REACTOR(77,124)\|MAFIC IGNEOUS ROCK(63,7)\|ROCK ASSEMBLAGE(59,1)\|ULTRAMAFIC IGNEOUS ROCK(58,7)\|PYROXENE RICH ORE(55,16)\|SEQUESTERING CARBON(51,6)\|REMAINING ORE PARTICLE(46,3)\|THERMODYNAMIC EQUILIBRIUM(44,2)\|OLIVINE(42,31)\|ORE(41,36)\|MINERAL ASSEMBLAGE(38,2)\|COMPLEX MINERALOGY(38,1)\|SERPENTINIZATION REACTION(33,23)\|GANGUE MINERAL(32,2)\|SEQUENTIAL CARBONATION(31,5)\|REMAINING ORE(30,16)\|GAS SEPARATOR(29,11)\|PYROXENE BEARING ORE(29,3)\|PRESELECTED SIZE(28,7)\|MAGNETIC SEPARATOR(27,7)\|PYROXENE(26,18)\|SCARCE METAL PRODUCTION(25,1)\|MAGNESITE(24,29)\|CARBON INTENSIVE(23,2)\|CARBON DIOXIDE(22,66)\|SCARCE METAL(22,15)\|CARBON DIOXIDE MINERALIZATION(22,5)\|PRODUCING MAGNETITE(22,4)\|HYDROGEN FORMATION(22,1)\|NATURAL GAS REFORMING(22,1)\|NATURAL GAS AVAILABILITY(20,1)\|CRUSHER(19,6)\|FLUID COMMUNICATION(19,3)\|HYDROGEN GAS(18,47)\|COMMINUTING(18,1)\|SIEVE(17,9)\|MAGNESIUM CARBONATE PRODUCTION(17,1)\|ROCK POWDER(16,6)\|CHEMISTRY(16,2)\|MAGNESIUM CARBONATE(15,31)\|PRECIOUS METAL(15,8)\|CHROMIUM(15,6)\|FORSTERITE MINERAL(15,4)\|GAS MIXTURE(15,2)\|COBALT(14,8)\|AMBIENT TEMPERATURE(14,4)\|COMMINUTED ROCK(14,4)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|PATHWAY(13,7)\|REACTION PRODUCT(12,22)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|DESIRED MINERAL(12,1)\|IRON OXIDE PRODUCTION(12,1)\|INORGANIC PHASE(11,13)\|UNREACTED ROCK ORE(11,3)\|GANGUE MATERIAL(11,2)\|WEATHERED MINERAL MINING(11,1)\|HYDROGEN PRODUCTION(10,13)\|CRUSHED GROUND ROCK(10,6)\|WASHER(10,3)\|NEUTRALIZE ACIDIFICATION(10,2)\|YOUNG OCEANIC CRUST(10,2)\|FAYALITE PRECONCENTRATION(10,1)\|FAYALITE SERPENTINIZATION(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|ECONOMIC VIABILITY(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|MAFIC IGNEOUS ROCK POTENTIAL(9,1)\|MAFIC ULTRAMAFIC ORE(9,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(9,1)\|MINERAL GRAIN COMMINUTION(9,1)\|SERPENTINIZATION REACTIONSSERPENTINIZATION REACTION(9,1)\|RESIDENCE TIME(8,21)\|SUPERCRITICAL CARBON DIOXIDE(8,3)\|UNREACTED ORE ROCK(8,2)\|CARBON MINERALIZATION KINETICS(8,1)\|HOMOGENIZED OLIVINE(8,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(8,1)\|OLIVINE ABUNDANCE(8,1)\|ORE CARBONATION DRIVEN COMMINUTION(8,1)\|PYROXENE MINERALOGY(8,1)\|RELEVANT CONSTITUENT ABUNDANCE(8,1)\|REVENUE ENTITLEMENT(8,1)\|ROCK DRIVER COMMINUTION(8,1)\|SERPENTINIZATION REACTION REACTIVITY(8,1)\|SERPENTINIZED ULTRAMAFIC ROCK(8,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(8,1)\|RARE EARTH ELEMENT(7,9)\|ATMOSPHERIC PRESSURE(7,6)\|CARBON NEUTRAL(7,6)\|COPPER BED(7,3)\|SEQUESTER CARBON DIOXIDE(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|BAND HEATER(7,2)\|BATCH EXPERIMENT(7,2)\|CERAMIC BRICK(7,2)\|FRACTIONATION FACTOR(7,2)\|GEOLOGICAL SITE(7,2)\|MAGNETITE MAGNESITE PRODUCTION(7,2)\|PYROLYSIS REACTION(7,2)\|RELEVANT COMPONENT(7,2)\|ROUGH PUMP(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|RESIDUAL IRON SILICATE(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBON DIOXIDE MINERALIZATION KINETICS(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|OLIVINE MINERAL PHASE(6,1)\|OLIVINE RICH DEPOSIT(6,1)\|OLIVINE RICH ORC(6,1)\|OLIVINE RICH ORE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|ALUMINUM OXIDE(5,9)\|REACTION CONDITION(5,6)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION(5,1)\|CIRCUMNEUTRAL PH(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|COPPER FILING HEATED BED(5,1)\|CRYOGENIC SEPARATION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL LATTICE(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE TEST(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REACTIONSDECARBONATION REACTION(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SIO DENSITY SEPARATION(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,25)\|HEAVY LIQUID SEPARATION(4,5)\|CARBON DIOXIDE GAS(4,4)\|MGCO(4,4)\|MGO(4,4)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE REACTIVITY(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|ENHANCE CARBON DIOXIDE SEQUESTRATION(4,2)\|ENHANCING PRODUCTION(4,2)\|IRON SILICATE PHASE(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|TAX CREDIT(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|COMMENSURATE CARBON DIOXIDE SEQUESTRATION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|INSOLUBLE MAGNESIUM CARBONATE(4,1)\|IRON RICH MINERAL(4,1)\|IRON SILICATE MINERAL PHASE(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM CARBONATE BULK(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE LOCATION(4,1)\|OLIVINEFAYALITE(4,1)\|OLIVINEFORSTERITEMG(4,1)\|PROCESSED ROCK(4,1)\|PYROXENEENSTATITEMG(4,1)\|PYROXENEFERROSILITE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|WATER OXYGEN FUGACITY(4,1)\|STOICHIOMETRIC RATIO(3,4)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SULFUR DIOXIDE(3,3)\|FLOWCHART BLOCK(3,2)\|FOSSIL FUEL COMBUSTION(3,2)\|STEAM METHANE REFORMING(3,2)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|DECADE(3,1)\|DISSOLUTION(3,1)\|ENHANCING CARBON DIOXIDE SEQUESTRATION(3,1)\|EXCESS UNREACTED CARBON DIOXIDE(3,1)\|EXPANSION VOLUME(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GASEOUS CARBON DIOXIDE(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|INCREASED MINERALIZATION(3,1)\|REACHING RESERVE(3,1)\|\|(US20240308843)\|MAGNETITE(100,58)\|ROCK(100,32)\|HYDROGEN PRODUCTION(100,13)\|ORE PARTICLE(100,12)\|HYDROGEN GENERATION(100,6)\|SEQUESTERING CARBON(100,6)\|REACTOR(75,123)\|MAGNESITE SEQUENTIAL CARBONATION(74,1)\|MAFIC IGNEOUS ROCK(63,7)\|ROCK ASSEMBLAGE(59,1)\|ULTRAMAFIC IGNEOUS ROCK(58,7)\|PYROXENE RICH ORE(55,16)\|REMAINING ORE PARTICLE(53,4)\|ORE(44,38)\|THERMODYNAMIC EQUILIBRIUM(44,2)\|OLIVINE(41,34)\|MINERAL ASSEMBLAGE(38,2)\|COMPLEX MINERALOGY(38,1)\|COMMINUTING(35,2)\|SERPENTINIZATION REACTION(34,25)\|REMAINING ORE(30,15)\|GAS SEPARATOR(30,11)\|PYROXENE BEARING ORE(29,3)\|PRESELECTED SIZE(28,7)\|MAGNETIC SEPARATOR(27,7)\|PYROXENE(26,20)\|SCARCE METAL PRODUCTION(25,1)\|CARBON INTENSIVE(23,2)\|SCARCE METAL(22,15)\|CARBON DIOXIDE MINERALIZATION(22,5)\|PRODUCING MAGNETITE(22,4)\|HYDROGEN FORMATION(22,1)\|NATURAL GAS REFORMING(22,1)\|CARBON DIOXIDE(21,90)\|MAGNESITE(21,28)\|NATURAL GAS AVAILABILITY(20,1)\|CRUSHER(19,6)\|FLUID COMMUNICATION(19,3)\|MAGNESIUM CARBONATE(18,35)\|SIEVE(17,9)\|SUPERCRITICAL CARBON DIOXIDE(17,3)\|HYDROGEN GAS(16,46)\|ROCK POWDER(16,6)\|CHEMISTRY(16,2)\|CHROMIUM(15,6)\|FORSTERITE MINERAL(15,4)\|COBALT(14,8)\|AMBIENT TEMPERATURE(14,4)\|COMMINUTED ROCK(14,4)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|PATHWAY(13,7)\|PRECIOUS METAL(13,7)\|REACTION PRODUCT(12,22)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|DESIRED MINERAL(12,1)\|UNREACTED ROCK ORE(11,3)\|GANGUE MATERIAL(11,2)\|DECARBONATION IGNEOUS MOLE(11,1)\|WEATHERED MINERAL MINING(11,1)\|CRUSHED GROUND ROCK(10,6)\|WASHER(10,3)\|NEUTRALIZE ACIDIFICATION(10,2)\|YOUNG OCEANIC CRUST(10,2)\|FAYALITE PRECONCENTRATION(10,1)\|FAYALITE SERPENTINIZATION(10,1)\|OLIVINE RICH ORC(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|ECONOMIC VIABILITY(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|MAFIC IGNEOUS ROCK POTENTIAL(9,1)\|MAFIC ULTRAMAFIC ORE(9,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(9,1)\|MINERAL GRAIN COMMINUTION(9,1)\|OLIVINE RICH DEPOSIT(9,1)\|OLIVINE RICH ORE(9,1)\|RESIDENCE TIME(8,21)\|UNREACTED ORE ROCK(8,2)\|CARBON MINERALIZATION KINETICS(8,1)\|GASEOUS CO2 DISSOLUTION(8,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(8,1)\|OLIVINE ABUNDANCE(8,1)\|ORE CARBONATION DRIVEN COMMINUTION(8,1)\|PYROXENE MINERALOGY(8,1)\|RELEVANT CONSTITUENT ABUNDANCE(8,1)\|REVENUE ENTITLEMENT(8,1)\|ROCK DRIVER COMMINUTION(8,1)\|SEQUESTRATION TAX CREDIT(8,1)\|SERPENTINIZATION REACTION REACTIVITY(8,1)\|SERPENTINIZED ULTRAMAFIC ROCK(8,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(8,1)\|RARE EARTH ELEMENT(7,9)\|ATMOSPHERIC PRESSURE(7,6)\|CARBON NEUTRAL(7,6)\|COPPER BED(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|BAND HEATER(7,2)\|BATCH EXPERIMENT(7,2)\|CERAMIC BRICK(7,2)\|FRACTIONATION FACTOR(7,2)\|GEOLOGICAL SITE(7,2)\|MAGNETITE MAGNESITE PRODUCTION(7,2)\|PYROLYSIS REACTION(7,2)\|RELEVANT COMPONENT(7,2)\|ROUGH PUMP(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STEAM METHANE REFORMING REACTION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|SUPERCRITICAL CO2(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|MGCO3(5,6)\|REACTION CONDITION(5,6)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|FE2SI2O(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CIRCUMNEUTRAL PH(5,1)\|CO2 MINERALIZATION RATE(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|COPPER FILING HEATED BED(5,1)\|CRYOGENIC SEPARATION(5,1)\|DECARBONATION REACTION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,25)\|SMALL SIZE FRACTION(4,6)\|HEAVY LIQUID SEPARATION(4,5)\|SODIUM BICARBONATE(4,5)\|FE3O(4,4)\|H2O(4,4)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|ENHANCING PRODUCTION(4,2)\|INORGANIC PHASE REACTION(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|MG2SIO(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|WATER OXYGEN FUGACITY(4,1)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|FLOWCHART BLOCK(3,2)\|FOSSIL FUEL COMBUSTION(3,2)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|DECADE(3,1)\|ENHANCING CARBON DIOXIDE(3,1)\|EXPANSION VOLUME(3,1)\|FE2SIO(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|INTENDED CARBONATION REACTION(3,1)\|REACHING RESERVE(3,1)\|\|(US12006212)\|REACTOR(100,131)\|MAGNETITE(100,58)\|ROCK(100,33)\|HYDROGEN(100,27)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,5)\|ORE(86,53)\|MAGNESITE SEQUENTIAL CARBONATION(77,1)\|MAFIC IGNEOUS ROCK(65,7)\|REMAINING ORE(61,19)\|ROCK ASSEMBLAGE(61,1)\|ULTRAMAFIC IGNEOUS ROCK(60,7)\|PYROXENE RICH ORE(58,16)\|COPPER FILING HEATED BED(52,3)\|OLIVINE(47,34)\|THERMODYNAMIC EQUILIBRIUM(46,2)\|COPPER FILING(45,3)\|WATER OXYGEN FUGACITY(44,3)\|OXYGEN FUGACITY(43,13)\|MINERAL ASSEMBLAGE(40,2)\|COMPLEX MINERALOGY(40,1)\|RECTOR(40,1)\|SERPENTINIZATION REACTION(34,23)\|PYROXENE(33,20)\|ORE PARTICLE(33,5)\|PRESELECTED SIZE(32,8)\|HEATED BED(32,3)\|AMBIENT TEMPERATURE(31,6)\|ACIDIC SOLUTION(30,4)\|PYROXENE BEARING ORE(30,3)\|MAGNESIUM CARBONATE(27,38)\|COMMINUTING(27,2)\|SUPERCRITICAL CARBON DIOXIDE(26,4)\|SCARCE METAL PRODUCTION(26,1)\|CARBON DIOXIDE(25,92)\|CARBON INTENSIVE(24,2)\|SCARCE METAL(23,15)\|CARBON DIOXIDE MINERALIZATION(23,5)\|PRODUCING MAGNETITE(23,4)\|HYDROGEN FORMATION(23,1)\|NATURAL GAS REFORMING(23,1)\|MAGNESITE(22,28)\|HYDROGEN GAS(21,48)\|NATURAL GAS AVAILABILITY(21,1)\|CHROMIUM(16,6)\|ROCK POWDER(16,6)\|CHEMISTRY(16,2)\|ATMOSPHERIC PRESSURE(15,8)\|COBALT(15,8)\|FORSTERITE MINERAL(15,4)\|PATHWAY(14,7)\|PRECIOUS METAL(14,7)\|COMMINUTED ROCK(14,4)\|OLIVINE RICH ORE(14,2)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|REACTION PRODUCT(13,22)\|INORGANIC PHASE(13,16)\|DESIRED MINERAL(13,1)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|WEATHERED MINERAL MINING(12,1)\|CRUSHED GROUND ROCK(11,6)\|UNREACTED ROCK ORE(11,3)\|GANGUE MATERIAL(11,2)\|LITHIUM(11,2)\|NEUTRALIZE ACIDIFICATION(11,2)\|YOUNG OCEANIC CRUST(11,2)\|FAYALITE PRECONCENTRATION(11,1)\|FAYALITE SERPENTINIZATION(11,1)\|RESIDENCE TIME(10,20)\|GAS SEPARATOR(10,9)\|MAGNETIC SEPARATOR(10,5)\|ECONOMIC VIABILITY(10,2)\|MAFIC IGNEOUS ROCK POTENTIAL(10,1)\|MAFIC ULTRAMAFIC ORE(10,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(10,1)\|MINERAL GRAIN COMMINUTION(10,1)\|OLIVINE RICH DEPOSIT(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|SIEVE(8,7)\|CARBON NEUTRAL(8,6)\|UNREACTED ORE ROCK(8,2)\|CARBON MINERALIZATION KINETICS(8,1)\|GASEOUS CO2 DISSOLUTION(8,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(8,1)\|MINERAL IGNEOUS MOLE(8,1)\|OLIVINE ABUNDANCE(8,1)\|ORE CARBONATION DRIVEN COMMINUTION(8,1)\|PYROXENE MINERALOGY(8,1)\|RELEVANT CONSTITUENT ABUNDANCE(8,1)\|REVENUE ENTITLEMENT(8,1)\|SEQUESTRATION TAX CREDIT(8,1)\|SERPENTINIZATION REACTION REACTIVITY(8,1)\|SERPENTINIZED ULTRAMAFIC ROCK(8,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(8,1)\|RARE EARTH ELEMENT(7,9)\|COPPER BED(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|BAND HEATER(7,2)\|BATCH EXPERIMENT(7,2)\|CERAMIC BRICK(7,2)\|CO2 MINERALIZATION RATE(7,2)\|FRACTIONATION FACTOR(7,2)\|GEOLOGICAL SITE(7,2)\|MAGNETITE MAGNESITE PRODUCTION(7,2)\|PYROLYSIS REACTION(7,2)\|RELEVANT COMPONENT(7,2)\|ROUGH PUMP(7,2)\|SUPERCRITICAL CO2(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STEAM METHANE REFORMING REACTION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|CRUSHER(6,4)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|MGCO3(5,6)\|REACTION CONDITION(5,6)\|HEAVY LIQUID SEPARATION(5,5)\|SODIUM BICARBONATE(5,5)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|CRYOGENIC SEPARATION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,25)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|ENHANCING PRODUCTION(4,2)\|FE2SI2O(4,2)\|FE2SIO(4,2)\|FLUID COMMUNICATION(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|MG2SIO(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PHASE DECARBONATION REACTION(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|HYDROGEN PRODUCTION(3,12)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|FLOWCHART BLOCK(3,2)\|FOSSIL FUEL COMBUSTION(3,2)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|DECADE(3,1)\|ENHANCING CARBON DIOXIDE(3,1)\|EXPANSION VOLUME(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|REACHING RESERVE(3,1)\|\|(US20230271827)\|REACTOR(100,132)\|MAGNETITE(100,60)\|ROCK(100,33)\|HYDROGEN(100,26)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,5)\|MAGNESITE SEQUENTIAL CARBONATION(78,1)\|ORE(76,50)\|ORE PARTICLE(71,9)\|REMAINING ORE(68,21)\|MAFIC IGNEOUS ROCK(66,7)\|ROCK ASSEMBLAGE(62,1)\|ULTRAMAFIC IGNEOUS ROCK(61,7)\|PYROXENE RICH ORE(58,16)\|OLIVINE(47,34)\|THERMODYNAMIC EQUILIBRIUM(46,2)\|MINERAL ASSEMBLAGE(40,2)\|COMPLEX MINERALOGY(40,1)\|COPPER FILING HEATED BED(39,3)\|PRESELECTED SIZE(38,10)\|SERPENTINIZATION REACTION(35,23)\|PYROXENE(34,20)\|WATER OXYGEN FUGACITY(34,3)\|GAS SEPARATOR(32,11)\|ACIDIC SOLUTION(30,4)\|PYROXENE BEARING ORE(30,3)\|MAGNETIC SEPARATOR(28,7)\|MAGNESIUM CARBONATE(27,38)\|COMMINUTING(27,2)\|SCARCE METAL PRODUCTION(27,1)\|CARBON DIOXIDE(25,92)\|SCARCE METAL(24,15)\|AMBIENT TEMPERATURE(24,5)\|CARBON INTENSIVE(24,2)\|CARBON DIOXIDE MINERALIZATION(23,5)\|PRODUCING MAGNETITE(23,4)\|HYDROGEN FORMATION(23,1)\|NATURAL GAS REFORMING(23,1)\|MAGNESITE(22,28)\|HYDROGEN GAS(21,48)\|NATURAL GAS AVAILABILITY(21,1)\|CRUSHER(20,6)\|FLUID COMMUNICATION(20,3)\|SIEVE(18,9)\|SUPERCRITICAL CARBON DIOXIDE(18,3)\|ROCK POWDER(17,6)\|CHROMIUM(16,6)\|CHEMISTRY(16,2)\|COBALT(15,8)\|FORSTERITE MINERAL(15,4)\|PATHWAY(14,7)\|PRECIOUS METAL(14,7)\|COMMINUTED ROCK(14,4)\|OLIVINE RICH ORE(14,2)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|REACTION PRODUCT(13,22)\|INORGANIC PHASE(13,16)\|DESIRED MINERAL(13,1)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|GANGUE MATERIAL(12,2)\|WEATHERED MINERAL MINING(12,1)\|ATMOSPHERIC PRESSURE(11,7)\|CRUSHED GROUND ROCK(11,6)\|UNREACTED ROCK ORE(11,3)\|LITHIUM(11,2)\|NEUTRALIZE ACIDIFICATION(11,2)\|YOUNG OCEANIC CRUST(11,2)\|FAYALITE PRECONCENTRATION(11,1)\|FAYALITE SERPENTINIZATION(11,1)\|RESIDENCE TIME(10,20)\|ECONOMIC VIABILITY(10,2)\|MAFIC IGNEOUS ROCK POTENTIAL(10,1)\|MAFIC ULTRAMAFIC ORE(10,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(10,1)\|MINERAL GRAIN COMMINUTION(10,1)\|OLIVINE RICH DEPOSIT(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|CARBON MINERALIZATION KINETICS(9,1)\|GASEOUS CO2 DISSOLUTION(9,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(9,1)\|MINERAL IGNEOUS MOLE(9,1)\|OLIVINE ABUNDANCE(9,1)\|ORE CARBONATION DRIVEN COMMINUTION(9,1)\|PYROXENE MINERALOGY(9,1)\|RELEVANT CONSTITUENT ABUNDANCE(9,1)\|REVENUE ENTITLEMENT(9,1)\|SEQUESTRATION TAX CREDIT(9,1)\|SERPENTINIZATION REACTION REACTIVITY(9,1)\|SERPENTINIZED ULTRAMAFIC ROCK(9,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(9,1)\|CARBON NEUTRAL(8,6)\|BAND HEATER(8,2)\|BATCH EXPERIMENT(8,2)\|CERAMIC BRICK(8,2)\|CO2 MINERALIZATION RATE(8,2)\|ENHANCED IMPLEMENTED ACCOUNTING(8,2)\|FRACTIONATION FACTOR(8,2)\|GEOLOGICAL SITE(8,2)\|MAGNETITE MAGNESITE PRODUCTION(8,2)\|PYROLYSIS REACTION(8,2)\|RELEVANT COMPONENT(8,2)\|ROUGH PUMP(8,2)\|UNREACTED ORE ROCK(8,2)\|RARE EARTH ELEMENT(7,9)\|COPPER BED(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|SUPERCRITICAL CO2(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STEAM METHANE REFORMING REACTION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|REACTION CONDITION(6,6)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|MGCO3(5,6)\|HEAVY LIQUID SEPARATION(5,5)\|SODIUM BICARBONATE(5,5)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CIRCUMNEUTRAL PH(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|CRYOGENIC SEPARATION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,25)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|FE2SI2O(4,2)\|FE2SIO(4,2)\|FLOWCHART BLOCK(4,2)\|FOSSIL FUEL COMBUSTION(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|MG2SIO(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PHASE DECARBONATION REACTION(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|COPPER ALLOY EFFORT(3,1)\|DECADE(3,1)\|EXPANSION VOLUME(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|INTENDED CARBONATION REACTION(3,1)\|IRON ORE NATURE(3,1)\|IRON RICH IRON ORE(3,1)\|IRON SILICATE MINERAL PHASE(3,1)\|KILOGRAM(3,1)\|LANTHANUM(3,1)\|REACHING RESERVE(3,1)\|\|(US20230102312)\|MAGNETITE(100,60)\|ROCK(100,33)\|HYDROGEN(100,26)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,5)\|REACTOR(99,134)\|MAGNESITE SEQUENTIAL CARBONATION(78,1)\|ORE(76,50)\|ORE PARTICLE(71,9)\|REMAINING ORE(68,21)\|MAFIC IGNEOUS ROCK(66,7)\|ROCK ASSEMBLAGE(62,1)\|ULTRAMAFIC IGNEOUS ROCK(61,7)\|PYROXENE RICH ORE(58,16)\|OLIVINE(47,35)\|THERMODYNAMIC EQUILIBRIUM(46,2)\|MINERAL ASSEMBLAGE(41,2)\|COPPER FILING HEATED BED(40,3)\|COMPLEX MINERALOGY(40,1)\|PRESELECTED SIZE(38,10)\|SERPENTINIZATION REACTION(35,23)\|PYROXENE(34,20)\|WATER OXYGEN FUGACITY(34,3)\|GAS SEPARATOR(31,12)\|ACIDIC SOLUTION(30,4)\|PYROXENE BEARING ORE(30,3)\|MAGNETIC SEPARATOR(28,7)\|MAGNESIUM CARBONATE(27,38)\|COMMINUTING(27,2)\|SCARCE METAL PRODUCTION(27,1)\|CARBON DIOXIDE(25,92)\|SCARCE METAL(24,15)\|AMBIENT TEMPERATURE(24,5)\|CARBON INTENSIVE(24,2)\|CARBON DIOXIDE MINERALIZATION(23,5)\|PRODUCING MAGNETITE(23,4)\|HYDROGEN FORMATION(23,1)\|NATURAL GAS REFORMING(23,1)\|MAGNESITE(22,28)\|HYDROGEN GAS(21,48)\|FLUID COMMUNICATION(21,3)\|NATURAL GAS AVAILABILITY(21,1)\|CRUSHER(20,6)\|SIEVE(18,9)\|SUPERCRITICAL CARBON DIOXIDE(18,3)\|ROCK POWDER(17,6)\|CHROMIUM(16,6)\|CHEMISTRY(16,2)\|COBALT(15,8)\|FORSTERITE MINERAL(15,4)\|PATHWAY(14,7)\|PRECIOUS METAL(14,7)\|COMMINUTED ROCK(14,4)\|OLIVINE RICH ORE(14,2)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|REACTION PRODUCT(13,22)\|INORGANIC PHASE(13,16)\|DESIRED MINERAL(13,1)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|GANGUE MATERIAL(12,2)\|WEATHERED MINERAL MINING(12,1)\|ATMOSPHERIC PRESSURE(11,7)\|CRUSHED GROUND ROCK(11,6)\|UNREACTED ROCK ORE(11,3)\|LITHIUM(11,2)\|NEUTRALIZE ACIDIFICATION(11,2)\|YOUNG OCEANIC CRUST(11,2)\|FAYALITE PRECONCENTRATION(11,1)\|FAYALITE SERPENTINIZATION(11,1)\|RESIDENCE TIME(10,20)\|ECONOMIC VIABILITY(10,2)\|MAFIC IGNEOUS ROCK POTENTIAL(10,1)\|MAFIC ULTRAMAFIC ORE(10,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(10,1)\|MINERAL GRAIN COMMINUTION(10,1)\|OLIVINE RICH DEPOSIT(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|CARBON MINERALIZATION KINETICS(9,1)\|GASEOUS CO2 DISSOLUTION(9,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(9,1)\|MINERAL IGNEOUS MOLE(9,1)\|OLIVINE ABUNDANCE(9,1)\|ORE CARBONATION DRIVEN COMMINUTION(9,1)\|OUTCROP QUARRYING(9,1)\|PYROXENE MINERALOGY(9,1)\|RELEVANT CONSTITUENT ABUNDANCE(9,1)\|REVENUE ENTITLEMENT(9,1)\|SEQUESTRATION TAX CREDIT(9,1)\|SERPENTINIZATION REACTION REACTIVITY(9,1)\|SERPENTINIZED ULTRAMAFIC ROCK(9,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(9,1)\|CARBON NEUTRAL(8,6)\|BAND HEATER(8,2)\|BATCH EXPERIMENT(8,2)\|CERAMIC BRICK(8,2)\|CO2 MINERALIZATION RATE(8,2)\|CRYOGENIC SEPARATION(8,2)\|FRACTIONATION FACTOR(8,2)\|GEOLOGICAL SITE(8,2)\|MAGNETITE MAGNESITE PRODUCTION(8,2)\|PYROLYSIS REACTION(8,2)\|RELEVANT COMPONENT(8,2)\|ROUGH PUMP(8,2)\|UNREACTED ORE ROCK(8,2)\|RARE EARTH ELEMENT(7,9)\|COPPER BED(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|SUPERCRITICAL CO2(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|ECONOMIC GEOLOGICAL HYDROGEN(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STOICHIOMETRIC ASSESSMENT(7,1)\|STOICHIOMETRIC MODELING(7,1)\|UNREACTED FAYALITE(7,1)\|GRAVITY SEPARATION(6,9)\|REACTOR VESSEL(6,9)\|REACTION CONDITION(6,6)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|RESIDUAL GAS ANALYZER(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|STOICHIOMETRIC CALCULATION(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|TOROIDAL FLUIDIZED BED(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|REACTION STEP(5,29)\|HEAVY LIQUID SEPARATION(5,6)\|MGCO3(5,6)\|SODIUM BICARBONATE(5,5)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|SOURCE ROCK COMMINUTION(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CIRCUMNEUTRAL PH(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ROTARY KILN(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|BRUCITE(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|FE2SI2O(4,2)\|FE2SIO(4,2)\|FLOWCHART BLOCK(4,2)\|FOSSIL FUEL COMBUSTION(4,2)\|MAGNESIUM COMPONENT(4,2)\|MG2SIO(4,2)\|STEAM METHANE REFORMING(4,2)\|TAILING(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|ELEVATED IRON CONTENT(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MIL NACL SALINE SOLUTION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PHASE DECARBONATION REACTION(4,1)\|POLLEN(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|VALENCE(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|MEMBRANE SEPARATION(3,3)\|PRELIMINARY RESULT(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|DECADE(3,1)\|EXPANSION VOLUME(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|INTENDED CARBONATION REACTION(3,1)\|IRON ORE NATURE(3,1)\|IRON RICH IRON ORE(3,1)\|IRON SILICATE MINERAL PHASE(3,1)\|KILOGRAM(3,1)\|REACHING RESERVE(3,1)\|\|(WO2023/007466)\|REACTOR(100,176)\|MAGNETITE(100,64)\|ROCK(100,34)\|HYDROGEN(100,25)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,7)\|H DROGEN(100,1)\|ORE(69,64)\|REMAINING ORE(69,31)\|ORE PARTICLE(57,11)\|MAGNESITE SEQUENTIAL CARBONATION(54,1)\|MAFIC IGNEOUS ROCK(45,7)\|ROCK ASSEMBLAGE(43,1)\|ULTRAMAFIC IGNEOUS ROCK(42,7)\|PYROXENE RICH ORE(40,16)\|OLIVINE(36,35)\|COMMINUTING(36,6)\|COPPER FILING HEATED BED(34,4)\|THERMODYNAMIC EQUILIBRIUM(32,2)\|RESIDENCE RIME(32,1)\|PRESELECTED SIZE(31,13)\|ACIDIC SOLUTION(31,7)\|WATER OXYGEN FUGACITY(29,4)\|PYROXENE BEARING ORE(29,3)\|CARBON DIOXIDE(28,113)\|PYROXENE(28,20)\|MINERAL ASSEMBLAGE(28,2)\|COMPLEX MINERALOGY(28,1)\|SERPENTINIZATION REACTION(24,24)\|AMBIENT TEMPERATURE(22,6)\|GAS SEPARATOR(21,12)\|MAGNESIUM CARBONATE(20,39)\|CHROMIUM(19,9)\|MAGNETIC SEPARATOR(19,7)\|SUPERCRITICAL CARBON DIOXIDE(19,3)\|SCARCE METAL PRODUCTION(18,1)\|HYDROGEN GAS(17,50)\|COBALT(17,11)\|CARBON INTENSIVE(17,2)\|SCARCE METAL(16,16)\|CARBON DIOXIDE MINERALIZATION(16,5)\|PRODUCING MAGNETITE(16,4)\|HYDROGEN FORMATION(16,1)\|NATURAL GAS REFORMING(16,1)\|MAGNESITE(15,29)\|CRUSHER(14,5)\|FLUID COMMUNICATION(14,3)\|NATURAL GAS AVAILABILITY(14,1)\|VAIYING REACTION CONDITION(14,1)\|RESIDENCE TIME(12,37)\|SIEVE(12,9)\|ROCK POWDER(11,6)\|LITHIUM(11,3)\|CHEMISTRY(11,2)\|ATMOSPHERIC PRESSURE(10,8)\|PATHWAY(10,7)\|COMMINUTED ROCK(10,4)\|FORSTERITE MINERAL(10,4)\|IMMENSE GEOLOGICAL SCALABILITY(10,1)\|REACTION PRODUCT(9,22)\|INORGANIC PHASE(9,17)\|PRECIOUS METAL(9,7)\|OLIVINE RICH ORE(9,2)\|DESIRED MINERAL(9,1)\|RARE EARTH ELEMENT(8,12)\|CARBON SEQUESTRATION(8,9)\|CARBONIZATION REACTION(8,5)\|UNREACTED ROCK ORE(8,3)\|GANGUE MATERIAL(8,2)\|WEATHERED MINERAL MINING(8,1)\|YOUNG OCEANIC CMST(8,1)\|CRUSHED GROUND ROCK(7,6)\|WASHER(7,3)\|ECONOMIC VIABILITY(7,2)\|NEUTRALIZE ACIDIFICATION(7,2)\|FAYALITE PRECONCENTRATION(7,1)\|FAYALITE SERPENTINIZATION(7,1)\|MAFIC IGNEOUS ROCK POTENTIAL(7,1)\|MAFIC ULTRAMAFIC ORE(7,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(7,1)\|MINERAL GRAIN COMMINUTION(7,1)\|OLIVINE RICH DEPOSIT(7,1)\|SUPERCRITICAL CAIBON DIOXIDE(7,1)\|ACCESSORY MINERAL COLLECTION(6,3)\|THERMOCOUPLE DETECTOR(6,3)\|AGGREGATE SUBSTITUTE(6,2)\|FERROSILITE MINERAL PHASE(6,2)\|MAFIC IGNEOUS ROCK SOURCE(6,2)\|PULVERIZED ROCK(6,2)\|RESIDUAL GANGUE(6,2)\|UNREACTED ORE ROCK(6,2)\|CARBON MINERALIZATION KINETICS(6,1)\|GASEOUS CO2 DISSOLUTION(6,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(6,1)\|OLIVINE ABUNDANCE(6,1)\|ORE CARBONATION DRIVEN COMMINUTION(6,1)\|OUTCROP QUARRYING(6,1)\|PYROXENE MINERALOGY(6,1)\|RELEVANT CONSTITUENT ABUNDANCE(6,1)\|REVENUE ENTITLEMENT(6,1)\|SEQUESTRATION TAX CREDIT(6,1)\|SERPENTINIZATION REACTION REACTIVITY(6,1)\|SERPENTINIZED ULTRAMAFIC ROCK(6,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(6,1)\|SMALL SIZE FRACTION(5,10)\|CARBON NEUTRAL(5,6)\|SRI GAS CHROMATOGRAPH(5,3)\|BAND HEATER(5,2)\|BATCH EXPERIMENT(5,2)\|CERAMIC BRICK(5,2)\|CRYOGENIC SEPARATION(5,2)\|FRACTIONATION FACTOR(5,2)\|GEOLOGICAL SITE(5,2)\|MAGNETITE MAGNESITE PRODUCTION(5,2)\|PYROLYSIS REACTION(5,2)\|RELEVANT COMPONENT(5,2)\|REMAINING ROCK GANGUE(5,2)\|ROUGH PUMP(5,2)\|ABIOGENIC METHANE FORMATION(5,1)\|CARBON MINERALIZATION EXPERIMENT(5,1)\|COMMINUTED ORE(5,1)\|EARTH CONTINENTAL CRUST(5,1)\|ECONOMIC GEOLOGICAL HYDROGEN(5,1)\|FORSTERITE AVAILABILITY(5,1)\|GANGUE MINERAL(5,1)\|GASEOUS CAIBON REACTION(5,1)\|HOMOGENIZED OLIVINE(5,1)\|HYDROGEN EVOLUTION KINETICS(5,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(5,1)\|NONCONDENSABLE FRACTION(5,1)\|REMAINING BULK ROCK GEOCHEMICAL(5,1)\|ROCK ORE BREAKDOWN(5,1)\|SCALABLE MAGNESITE(5,1)\|SCIENTIFIC SUPPLIER(5,1)\|SEQUENTIAL CARBONIZATION(5,1)\|STOICHIOMETRIC ASSESSMENT(5,1)\|STOICHIOMETRIC MODELING(5,1)\|ULTRAMAFRC ROCK(5,1)\|UNREACTED FAYALITE(5,1)\|YOUNG OCEANIC CRUST(5,1)\|GRAVITY SEPARATION(4,9)\|REACTOR VESSEL(4,9)\|FERTILIZER(4,4)\|PRESELECTED TEMPERATURE(4,4)\|ROTARY KILN(4,4)\|STANDARD OMEGA(4,4)\|ACCOUNTING(4,3)\|DIHYDROGEN SULFIDE(4,3)\|ELECTRICITY(4,3)\|EVEN CARBON NEGATIVE(4,3)\|IRON RICH SILICATE MINERAL(4,3)\|LANDFILL(4,3)\|NATURAL REACTION(4,3)\|REMAINING ROCK ORE(4,3)\|SEQUENTIAL REACTION(4,3)\|SOURCE ROCK COMMINUTION(4,3)\|VALUABLE CONSTITUENT(4,3)\|COMPETITION(4,2)\|COPPER BED(4,2)\|OLIVINE WASTE STREAM(4,2)\|OMEGA K WIRE THERMOCOUPLE(4,2)\|RESIDUAL GAS ANALYZER(4,2)\|AGGREGATE SALE(4,1)\|AMBIENT OXYGEN FUGACITY(4,1)\|CARBONATE MINERALIZATION(4,1)\|COMMENSURATE LY(4,1)\|ENABLED EXPERIMENTATION(4,1)\|ENSTATITE MINERAL(4,1)\|GOVERNMENT MANDATED REGULATION(4,1)\|MAGNETITE RECOVERY(4,1)\|MID OCEANIC RIDGE(4,1)\|MINERAL BREAKDOWN(4,1)\|MITIGATE ATMOSPHERIC RELEASE(4,1)\|PROLIFIC OCCURRENCE(4,1)\|QUARRYING CONCEPT(4,1)\|REACTION SEQUENTIAL ORDERING(4,1)\|ROCK HAMMER(4,1)\|ROCK METRIC TON(4,1)\|SEQUENTIAL SERPENTINIZATION REACTION(4,1)\|STEAM REFORMER(4,1)\|STOICHIOMETRIC CALCULATION(4,1)\|THERMOCHEMICAL DRIVER(4,1)\|TOROIDAL FLUIDIZED BED(4,1)\|ULTRAMAFIC ROCK BULK SAMPLE(4,1)\|REACTION STEP(3,29)\|HEAVY LIQUID SEPARATION(3,6)\|SODIUM BICARBONATE(3,5)\|POTASSIUM HYDROXIDE(3,4)\|PSI PRESSURE GAUGE(3,4)\|ACCESSORY MINERAL PHASE(3,2)\|AGRICULTURAL LIME(3,2)\|BRUCITE(3,2)\|CARBON DIOXIDE INTRODUCTION(3,2)\|CRUSHING(3,2)\|ELECTROLYSIS(3,2)\|MAGNESIUM COMPONENT(3,2)\|MAGNETITE REACTION PRODUCT(3,2)\|TAILING(3,2)\|ULTRAMAFIC AGGREGATE MATERIAL(3,2)\|UNREACTED CARBON DIOXIDE(3,2)\|ACCESSORY OXIDE(3,1)\|ACTIVE QUARRY(3,1)\|ANTIGORITE REACTION(3,1)\|ASBESTOS BACK DEHYDRATION(3,1)\|BEST MECHANISTIC REACTION(3,1)\|BULK ORE(3,1)\|CARBON ECONOMY PURSUIT(3,1)\|CARBON MINERALIZATION KINETIC RATE(3,1)\|CARBON MINERALIZATION RATE(3,1)\|CARBON NEGATIVE CONCRETE FDLER(3,1)\|CARBON NEUTRAL PURSUIT(3,1)\|CARBON SEQUESTERING CARBONATION REACTION(3,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(3,1)\|CEMENT MANUFACTURING(3,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(3,1)\|CIRCUMNEUTRAL PH(3,1)\|CO2 OCCURRENCE(3,1)\|COMPETING REACTION OCCURRENCE(3,1)\|COMPLEX CHEMISTRY(3,1)\|CONCENTRATE SCARCE METAL(3,1)\|CONTAMINANT GAS(3,1)\|CRUSHED GROUND ORE(3,1)\|DENSER IRON SILICATE(3,1)\|DERIVATIVE UTILIZATION(3,1)\|DESCRIPTIVE SENSE(3,1)\|DEVELOPMENT EFFORT(3,1)\|DISPOSITIONING(3,1)\|ELEVATED IRON CONTENT(3,1)\|ENHANCE KINETICS(3,1)\|ENHANCED MAGNETITE PRODUCTION(3,1)\|EXPERIMENTAL RUN(3,1)\|EXPLOIT GEOLOGICAL FORMATION(3,1)\|EXPLOITATION(3,1)\|EXTRACT HYDROGEN(3,1)\|FAYALITE HYDRATION REACTION(3,1)\|FC SBO(3,1)\|FC SFO(3,1)\|FLUID GEOCHEMISTRY(3,1)\|FLUID SAMPLING PORT(3,1)\|FORSTEIITE COMPONENT(3,1)\|FORSTERITE REACTION(3,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(3,1)\|GENERIC SENSE(3,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(3,1)\|GRAVITY SEPARATOR(3,1)\|GREEN AMMONIA(3,1)\|GREEN GOLDEN HYDROGEN(3,1)\|GROUNDWATER TREATMENT(3,1)\|HYDROGEN GENERATION COPRODUCT(3,1)\|IRON RICH IRON SILICA(3,1)\|IRON RICH MINERAL(3,1)\|IRON RICH OLIVINE(3,1)\|LABILE CARBON(3,1)\|MACHINERY PLACEMENT(3,1)\|MAGNESITE FORMATION(3,1)\|MAGNESITE GENERATION(3,1)\|MAGNESITE VALUE UTILIZATION(3,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(3,1)\|MAGNESIUM RICH SILICATE MINERAL(3,1)\|MAGNESIUM SILICATE CONVERSION(3,1)\|MAGNETITE PARTICLE(3,1)\|MAGNETITE REMOVAL(3,1)\|MAGNETITE YIELD(3,1)\|MEANINGFUL BENEFIT(3,1)\|METHANE CONVERSION(3,1)\|MG SIO(3,1)\|MIL NACL SALINE SOLUTION(3,1)\|MILDLY ACIDIC CONDITION(3,1)\|MILDLY ACIDIC SOLUTION(3,1)\|MINERAL PROCESSING(3,1)\|MINERAL SECONDARY RECOVERY(3,1)\|MINERAL SLAG(3,1)\|MUNICIPAL WASTEWATER TREATMENT(3,1)\|OLIVINE MINERAL PHASE(3,1)\|OLIVINE TEST(3,1)\|PH AMENDMENT(3,1)\|PHASE MINERAL UNITY(3,1)\|PREEVACUATED SAMPLE CHAMBER(3,1)\|PRIMARY DIFFERENTIATOR(3,1)\|PROCESSED ROCK(3,1)\|PYROXENE BEARING LOCALITY(3,1)\|REMAINING ROCK UNREACTED ORE(3,1)\|REMAINING UNREACTED ORE(3,1)\|RESIDUAL IRON SILICATE(3,1)\|RESIDUAL OLIVINE(3,1)\|ROBUST DEPOSIT(3,1)\|ROCK CONTENT(3,1)\|ROCK PREPARATION PHASE(3,1)\|SCARCE METAL RESOURCE(3,1)\|SEALED REACTOR(3,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(3,1)\|SERPENTINIZATION HYDRATION REACTION(3,1)\|SERPENTINIZATION REACTION KINETIC RATE(3,1)\|SERPENTINIZATION REACTION PHASE(3,1)\|SOHD REACTION PRODUCT(3,1)\|SOLUTION GLOBAL APPLICABILITY(3,1)\|SPEX BALL MILL(3,1)\|SR QUADRUPOLE MASS SPECTROMETER(3,1)\|STANDARD GEOTHERMOMETER(3,1)\|STOICHIOMETRIC PROPORTION(3,1)\|STONE AGGREGATE FORMATION(3,1)\|TARGET PRODUCTION(3,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(3,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(3,1)\|ULTRAMAFIC FORMATION(3,1)\|UNDESIRED MINERAL SPECIES(3,1)\|UNIFORM SIZING(3,1)\|VALENCE(3,1)\|VARIABLE OXYGEN FUGACITY(3,1)\|VISIBLE OLIVINE(3,1)\|WATER LOWERED OXYGEN FUGACITY(3,1)\|MAGNESIUM OXIDE(2,4)\|STOICHIOMETRIC RATIO(2,4)\|CARBON DIOXIDE GAS(2,3)\|FACILITY(2,3)\|GRINDER(2,3)\|HYDROGEN GAS EVOLUTION(2,3)\|IRON SILICATE PHASE(2,3)\|MEMBRANE SEPARATION(2,3)\|PRELIMINARY RESULT(2,3)\|SULFUR DIOXIDE(2,3)\|FLOWCHART BLOCK(2,2)\|FOSSIL FUEL COMBUSTION(2,2)\|STEAM METHANE REFORMING(2,2)\|ABIOTIC HYDROGEN PRODUCTION(2,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(2,1)\|ALUMINOSILICATE(2,1)\|AMPLIFICATION(2,1)\|ATMOSPHERIC CONDITION(2,1)\|ATTRACTION(2,1)\|BATCH CONDITION(2,1)\|CARBON DIOXIDE EMISSION(2,1)\|CARBON DIOXIDE PURITY(2,1)\|CARBON DIOXIDE REACTIVITY(2,1)\|CARBON NEGATIVE CONCRETE FILLER(2,1)\|CARBON SEQUESTRATION CAPACITY(2,1)\|CRASHER(2,1)\|DECADE(2,1)\|EXPANSION VOLUME(2,1)\|FINE POWDER(2,1)\|FLUID CHEMISTRY(2,1)\|GEOLOGICAL SOURCE(2,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(2,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(2,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(2,1)\|INCREASED MINERALIZATION(2,1)\|INCREASED REACTIVITY(2,1)\|REACHING RESERVE(2,1)\|\|(JP2024528907)\|REACTOR(100,242)\|ORE(100,85)\|ROCK(100,54)\|MAGNETITE(100,34)\|HYDROGEN PRODUCTION(100,24)\|PRESELECTED SIZE(100,22)\|PYROXENE(100,22)\|INLET(100,21)\|KANLANITE(100,16)\|ORE PARTICLE(100,12)\|CRUSHER(100,9)\|SIEVE(100,9)\|CARBON(100,7)\|ISOLATING CARBON(100,7)\|OUTLET(100,6)\|SUPPLY SOURCE(100,5)\|RECEIVE ONLY ORE PARTICLE(100,1)\|ORE INTRODUCTION(71,4)\|REMAINING ORE(64,38)\|OBTAINING ORE(62,3)\|MAGNETITE ORE(58,44)\|ROUGH STONE(57,3)\|MINERAL AGGREGATE COMPLEX(37,1)\|PRODUCING MAGNETITE ORE(34,2)\|GANGLIOLITE SUBSTANCE(34,1)\|THERMODYNAMIC EQUILIBRIUM(33,2)\|ULTRAMAGNETIC IGNEOUS ROCK(32,2)\|MAGNETITE ATTRACTION(32,1)\|ORE GRINDING(31,2)\|MAGNETIC ORE(31,1)\|CARBON DIOXIDE(30,147)\|SEQUENTIAL CARBONATION REACTION(30,1)\|MINERAL AGGREGATE(29,2)\|SIFTING ORE(29,1)\|ACIDIC SOLUTION(28,11)\|WATER OXYGEN FUGACITY(27,6)\|PRODUCING MAGNESIUM CARBONATE(27,2)\|MAGNESIUM SILICATE CONVERSION(26,1)\|FLUID COMMUNICATION(25,3)\|APPENDIX(24,103)\|REMAINING ROCK(24,5)\|ORE PARTICLE COATING(24,1)\|CARBON DIOXIDE PRESSURE(22,31)\|CARBONATION REACTION(22,15)\|AMBIENT TEMPERATURE(22,9)\|SERPENTINIZATION(22,7)\|SEQUESTERING CARBON(22,1)\|FINE POWDER(21,1)\|SCENARIO(21,1)\|MAGNETIC SEPARATOR(20,7)\|RAW STONE(20,6)\|CARBONATE MINERAL(20,4)\|MAGNESITE(19,31)\|CHROMIUM(19,11)\|ORE TREATMENT(19,1)\|MAGNESIUM CARBONATE(18,41)\|SUPERCRITICAL CARBON DIOXIDE(18,6)\|COBALT(17,13)\|CARBON DIOXIDE MINERALIZATION(17,5)\|PYROXITE(17,2)\|QUANLANITE(17,1)\|REMAINING IRON SILICATE(17,1)\|HYDROGEN GAS(16,55)\|GRINDING(16,6)\|YOUNG MARINE CRUST(16,5)\|GAS SEPARATOR(15,10)\|CRUSHING(15,4)\|REMOVING OXYGEN(15,4)\|PHYLLOITE(15,1)\|CARBON ISOLATION(14,5)\|CAMLANITE(14,3)\|IRON SILICATE(13,21)\|SMALL SIZED PIECE(12,7)\|PYROXENE RICH ORE(12,6)\|ROCK MASS(12,4)\|PARTICLE DIAMETER(12,1)\|HYDRATION REACTION(11,9)\|LITHIUM(11,4)\|BITTERN KANLANITE MINERAL(11,3)\|BITTERN KANLAN MINERAL REACTIVITY(11,1)\|USEFUL COMPONENT REMOVAL(11,1)\|REACTION PRODUCT(10,22)\|INORGANIC PHASE(10,17)\|ATMOSPHERIC PRESSURE(10,11)\|CARBONIZATION REACTION(10,7)\|MAGNESIUM SILICATE(10,3)\|ULTRAFINE IGNEOUS ROCK(10,2)\|BITTEROUS ROCK RESERVE(10,1)\|FERROUS SILICEOUS PYROXENE(10,1)\|IRON KANLANITE MINERAL PRECONCENTRATION(10,1)\|STUBBORN PYROXENE STONE(10,1)\|RESIDENCE TIME(9,53)\|REACTION STEP(9,32)\|ROCK POWDER(9,4)\|CLEANER(9,3)\|FERROUS KANLANITE(9,3)\|MAGNETITE ORE PRODUCTION(9,3)\|SERPENTINE LITHOTRIZATION REACTION(9,2)\|SUPERFINE MAFIC IGNEOUS ROCK(9,1)\|RARE EARTH ELEMENT(8,14)\|DENSITY SEPARATION(8,7)\|UTILITY COMPONENT(8,3)\|IRON SILICEOUS STONE MINERAL(8,2)\|PULVERIZED ROCK(8,2)\|SUPERMAFIC ROCK(8,2)\|ULTRAMAGNETIC ROCK(8,2)\|ULTRAMUTITE ROCK(8,2)\|BITTERN KANRAN STONE MINERAL(8,1)\|HOMOGENIZED KANLANITE MINERAL(8,1)\|IRON SILICENE PYROXENE MINERAL(8,1)\|MAGNESITE RICH ORE(8,1)\|QUARRIED KANLANITE(8,1)\|REACTION RESULT(8,1)\|ROBUST MAFIC DEPOSIT(8,1)\|ROCK AGGREGATE SERPENTINIZATION REACTION(8,1)\|WEATHERED MINERAL EXTRACTION(8,1)\|RARE METAL(7,22)\|IRON SILICATE MINERAL(7,4)\|RETENTION TIME(7,3)\|ROCK MINERAL(7,3)\|SMALL SIZED FRAGMENT(7,3)\|THERMOCOUPLE DETECTOR(7,3)\|UNREACTED ROCK ORE(7,3)\|STONE AGGREGATE(7,2)\|BITTERNESS SUPERBITTEROUS ORE(7,1)\|ULTRAMAGNETIC MAGNOLITE(7,1)\|CARBON NEUTRAL(6,6)\|CENTRAL RIDGE(6,5)\|NONBIOLOGICAL HYDROGEN GENERATION(6,4)\|SMALL PIECE(6,4)\|CHEMICAL PROPERTY(6,2)\|FERROUS SILICATE(6,2)\|FRACTIONAL COEFFICIENT(6,2)\|MAGNETITE MAGNESITE GENERATION(6,2)\|OXYGEN FUGASITY(6,2)\|BIGENTOUS PYROXITE(6,1)\|BIGENTRIC PYROXENE(6,1)\|BITTERN CALCINITE(6,1)\|BITTERN KANOLITE(6,1)\|BITTEROUS ROCK ORE(6,1)\|IRON CAMELANITE MINERAL(6,1)\|IRON KANLAN ROCK(6,1)\|KINETIC LAW STUDY(6,1)\|MAGNETITE ORE GENERATION(6,1)\|NEUTRALIZE ACIDIFICATION(6,1)\|OXYGEN FUGA CITY(6,1)\|PROMOTING SERPENTINIZATION(6,1)\|ROCK PULVERIZATION(6,1)\|SERPENTINIZING REACTION REACTIVITY(6,1)\|SOLID MATERIAL(6,1)\|STUBBLE PYROXENE(6,1)\|STUBBORN CALCINITE(6,1)\|STUBBORN TERMITE(6,1)\|ULTRAFINE METEOROID(6,1)\|ULTRAMERETIC ROCK BULK SAMPLE(6,1)\|UNREACTED IRON KANLANITE(6,1)\|VOLUNTARY PRIVATE SECTOR EFFORT(6,1)\|CARBON NEGATIVE(5,8)\|COPPER FLOOR(5,3)\|PRODUCTION PROMOTION(5,3)\|SRI GAS CHROMATOGRAPH(5,3)\|BAND HEATER(5,2)\|BATCH EXPERIMENT(5,2)\|CERAMIC BRICK(5,2)\|CO2 MINERALIZATION RATE(5,2)\|GASEOUS CO2(5,2)\|GEOLOGICAL SITE(5,2)\|INORGANIC PARTICLE(5,2)\|IRON KANOLITE MINERAL(5,2)\|IRON SILICEOUS MINERAL PHASE(5,2)\|MAGNESITE MINERAL PHASE(5,2)\|MAGNESITE PRODUCTION(5,2)\|RESIDUAL VEIN(5,2)\|ROUGH PUMP(5,2)\|SEPARATING ROCK(5,2)\|ARBITRARY SLAG SUBSTANCE(5,1)\|BITTERN KANRAN MINERAL(5,1)\|BITTERN LANTHANUM MINERAL(5,1)\|CARBON MINERALIZATION EXPERIMENT(5,1)\|CARBONATION REACTION ACCELERATOR(5,1)\|DEHYDRATING ASBESTOS(5,1)\|EARTH CONTINENTAL CRUST(5,1)\|ECONOMIC GEOLOGICAL HYDROGEN(5,1)\|EXPANDABLE MAGNESITE FORMATION(5,1)\|FERROUS CALCINITE REACTION(5,1)\|GANGOLITE MINERAL(5,1)\|IRON SERPENTINIZATION(5,1)\|IRON SILICA PYROXENE(5,1)\|MINERAL CARBONATE(5,1)\|MUNICIPAL SEWAGE(5,1)\|NEUTRALIZING ACIDIFICATION(5,1)\|OBLIQUE TERMITE(5,1)\|PULSATING STONE(5,1)\|REMAINING BULK ROCK GEOCHEMICAL(5,1)\|SILICEOUS ROCK(5,1)\|STEAM METHANE REFORMING REACTION(5,1)\|STOICHIOMETRIC MODELING(5,1)\|STOICHIOMETRIC SERPENTINE REACTION(5,1)\|SUPERBITTERLIKE ROCK(5,1)\|SUPERBITTEROUS ROCK(5,1)\|SUPERMUNITIC ROCK(5,1)\|ULTRAMAGNETIC ORE(5,1)\|ULTRAMATERIOUS ROCK(5,1)\|ULTRAMERETIC ROCK ORE(5,1)\|GRAVITY SEPARATION(4,8)\|HEAVY LIQUID SEPARATION(4,6)\|REACTION CONDITION(4,6)\|FERTILIZER(4,4)\|GRAVEL(4,4)\|DIHYDROGEN SULFIDE(4,3)\|IRON RICH SILICATE MINERAL(4,3)\|LANDFILL(4,3)\|NATURAL REACTION(4,3)\|PHANOLITE(4,3)\|REMAINING ROCK ORE(4,3)\|SEQUENTIAL REACTION(4,3)\|STRATUM(4,3)\|CARBON DIOXIDE SEQUESTRATION(4,2)\|CARBON MINERALIZATION RATE(4,2)\|COMPETITIVE REACTION(4,2)\|OMEGA K WIRE THERMOCOUPLE(4,2)\|RESIDUAL GAS ANALYZER(4,2)\|WEAKLY ACIDIC SOLUTION(4,2)\|AGGREGATE SALE(4,1)\|AMBIENT OXYGEN FUGACITY(4,1)\|ANTIGOLITE REACTION(4,1)\|BITTEROUS ROCK COMPONENT(4,1)\|BULK ORE(4,1)\|CARBON MINERALIZATION KINETIC RATE(4,1)\|CARBONATED MINERAL PHASE(4,1)\|CLEAN ORE(4,1)\|CO2 REACTION(4,1)\|COPPER SCRAP FLOOR(4,1)\|CRUSHED ORE(4,1)\|EXPOSED IRON KANLANITE(4,1)\|EXTRACTING HYDROGEN(4,1)\|FLUID GEOCHEMISTRY(4,1)\|GOVERNMENT IMPOSED REGULATION(4,1)\|GRAVITY SEPARATOR(4,1)\|GROUNDWATER TREATMENT(4,1)\|HARMFUL MINERAL PHASE(4,1)\|HYPOXIA FUGACITY WATER(4,1)\|HYPOXIC FUGACITY WATER(4,1)\|INTRODUCING ROCK(4,1)\|IRON KANLANITE MINERAL PHASE(4,1)\|IRON KANOLANITE(4,1)\|IRON PYROXENE(4,1)\|IRON RICH KANLANITE(4,1)\|IRON SILICANITE(4,1)\|IRON TERMITE(4,1)\|ISOLATION TAX CREDIT(4,1)\|KANLAN STONE TEST SAMPLE(4,1)\|KANLANITE RICH ORE(4,1)\|MAFIC IGNEOUS ROCK SOURCE(4,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(4,1)\|MAGNETITE PARTICLE(4,1)\|MAGNETITE YIELD(4,1)\|MEANINGFUL BENEFIT(4,1)\|MINERAL SLAG(4,1)\|ORE RESIDUE(4,1)\|ORIGIN GENE(4,1)\|OXYGEN FUGATIVITY(4,1)\|PAST FEW DECADE(4,1)\|PURITY CO2(4,1)\|PYROLYSIS REACTION(4,1)\|REACTING CRUSHED GROUND ROCK(4,1)\|REACTIVITY BENEFIT(4,1)\|REMAINING ROCK UNREACTED ORE(4,1)\|REMAINING UNREACTED MINERAL(4,1)\|REMAINING UNREACTED ORE ROCK(4,1)\|ROCK HAMMER(4,1)\|ROCK METRIC TON(4,1)\|ROCK ORE DECOMPOSITION(4,1)\|ROCK PARTICLE(4,1)\|SCIENTIFIC SUPPLIER(4,1)\|SECTION REACTION STEP(4,1)\|SENDING DEVICE REMAINING ORE(4,1)\|SEQUENTIAL CARBON ISOLATION CARBONATION(4,1)\|SEQUENTIAL CARBONIZATION(4,1)\|SEQUENTIAL SERPENTINIZATION REACTION(4,1)\|SOIL KANLANITE(4,1)\|SOLUTION GLOBAL APPLICABILITY(4,1)\|SPEX BALL MILL(4,1)\|STANDARD GEOTHERMAL ANALYZER(4,1)\|STOICHIOMETRIC CALCULATION(4,1)\|STOICHIOMETRIC EVALUATION(4,1)\|SUPER BITTEROUS ROCK(4,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(4,1)\|ULTRAMAFIC DEPOSIT(4,1)\|VISIBLE KANLANITE(4,1)\|WATER OXYGEN FUGAL CITY(4,1)\|GRINDING MACHINE(3,5)\|SODIUM BICARBONATE(3,5)\|POTASSIUM HYDROXIDE(3,4)\|SODIUM HYDROXIDE(3,4)\|PATHWAY(3,3)\|AGRICULTURAL LIME(3,2)\|ATTACHMENT DRAWING(3,2)\|BLUE SITE(3,2)\|CARBON NEGATIVE CONCRETE FILLER(3,2)\|ELECTROLYSIS(3,2)\|GANGUE(3,2)\|MAGNESIUM COMPONENT(3,2)\|MG2SIO(3,2)\|PRESELECTED TEMPERATURE(3,2)\|SINK(3,2)\|SUBSTITUTE(3,2)\|SUPERCRITICAL CO2(3,2)\|TERMIITE(3,2)\|UNREACTED CARBON DIOXIDE(3,2)\|ACCELERATE REMOVAL(3,1)\|ACTIVE QUARRY(3,1)\|AIRTIGHT STAINLESS STEEL(3,1)\|ARBITRARY ACTION(3,1)\|CARBON DIOXIDE SEGREGATION(3,1)\|CARBON INTENSIVE CONSTRAINT(3,1)\|CARBON NEUTRAL PURSUIT(3,1)\|CARBONATION SERPENTINE REACTION PRODUCT(3,1)\|CEMENT PRODUCTION(3,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(3,1)\|CO2 GENERATION(3,1)\|COMPONENT ABUNDANCE(3,1)\|CRUSHED GROUND ORE(3,1)\|DEBATE(3,1)\|DEEP COLD SEPARATION(3,1)\|DENSE IRON SILICATE(3,1)\|DEVELOPMENT EFFORT(3,1)\|EXPLANATORY SENSE(3,1)\|FINE PARTICULATE(3,1)\|FLUID SAMPLING PORT(3,1)\|GAS ALLICOTE(3,1)\|GASEOUS CARBON DIOXIDE ISOLATION(3,1)\|GENERATING MAGNETITE(3,1)\|GENERATING ORE(3,1)\|GEOCHEMICAL CONDITION(3,1)\|GREEN AMMONIA(3,1)\|GREEN GOLDEN HYDROGEN(3,1)\|IMPURITY GAS(3,1)\|IRON KANRAN MINERAL PHASE(3,1)\|IRON ORE RICH(3,1)\|IRON RICH IRON SILICA(3,1)\|IRON RICH MINERAL(3,1)\|ISOLATING HYDROGEN(3,1)\|MAGNESITE VALUE(3,1)\|MAGNESIUM RICH SILICATE MINERAL(3,1)\|MAGNETITE PRODUCTION(3,1)\|MAGNETITE REMOVAL(3,1)\|METHANE CONVERSION(3,1)\|METHANE FORMATION(3,1)\|OBTAINING ROCK(3,1)\|ORE OVER TIME(3,1)\|OXYGEN FUGAL CITY WATER(3,1)\|PASS ORE PARTICLE(3,1)\|PRODUCING MAGNETITE(3,1)\|REMAINING ROCK PULSATE(3,1)\|ROCK CONTENT(3,1)\|ROCK KG(3,1)\|ROCK PREPARATION PHASE(3,1)\|SEALED REACTOR(3,1)\|SEPARATING SIO2(3,1)\|SERPENTINE FORMATION REACTION(3,1)\|SERPENTINIZATION HYDRATION(3,1)\|SR QUADRUPOLE MASS SPECTROMETER(3,1)\|STONE TREATMENT(3,1)\|SUBPHASE COMPETITIVE PHASE(3,1)\|TARGET PRODUCTION(3,1)\|TOTAL CARBON MINERALIZATION(3,1)\|TRACE CO2(3,1)\|ULTRAMUTITE SOURCE(3,1)\|UNEXTRACTABLE MINERAL PHASE LAYER(3,1)\|URBAN SEWAGE TREATMENT(3,1)\|WASTE FLOWING KANLANITE(3,1)\|WATER OXYGEN FUMARICITY(3,1)\|WEAKLY ACIDIC AQUEOUS SOLUTION(3,1)\|WEAKLY ACIDIC CONDITION(3,1)\|STOICHIOMETRIC RATIO(2,5)\|GEOLOGICAL LAYER(2,4)\|CARBON DIOXIDE GAS(2,3)\|FLUIDIZED BED(2,3)\|IRON SILICATE PHASE(2,3)\|PRELIMINARY RESULT(2,3)\|ROTARY KILN(2,3)\|SO2(2,3)\|SULFUR DIOXIDE(2,3)\|CASTING(2,2)\|FLOWCHART BLOCK(2,2)\|FOSSIL FUEL COMBUSTION(2,2)\|ACCESSORY MINERAL PHASE(2,1)\|ACCOUNTING(2,1)\|ALUMINOSILICATE(2,1)\|ATTRACTION(2,1)\|BARGE(2,1)\|BATCH CONDITION(2,1)\|CANLANITE(2,1)\|CARBON DIOXIDE EMISSION(2,1)\|CARBON DIOXIDE INTRODUCTION(2,1)\|CARBON DIOXIDE PURITY(2,1)\|CARBON DIOXIDE REACTIVITY(2,1)\|CARBON SEQUESTRATION CAPACITY(2,1)\|CHANGING PH(2,1)\|CO2 RATIO(2,1)\|CONCENTRATE(2,1)\|DIFFERENTIATOR(2,1)\|DISPOSAL(2,1)\|DIVERSE CHEMICAL PROPERTY FORMATION(2,1)\|FE SILICITE(2,1)\|FE2SI2O(2,1)\|FE2SIO(2,1)\|FLUID CHEMISTRY(2,1)\|GAS PURGE ACTION(2,1)\|GAS REACTION(2,1)\|GASEOUS CARBON DIOXIDE REACTION(2,1)\|GEOLOGICAL SOURCE(2,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(2,1)\|\|(IN202417013808)\|REACTOR(100,174)\|MAGNETITE(100,64)\|ROCK(100,35)\|HYDROGEN(100,25)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,7)\|H DROGEN(100,1)\|ORE(69,64)\|REMAINING ORE(69,31)\|ORE PARTICLE(57,11)\|MAGNESITE SEQUENTIAL CARBONATION(53,1)\|MAFIC IGNEOUS ROCK(45,7)\|ROCK ASSEMBLAGE(43,1)\|ULTRAMAFIC IGNEOUS ROCK(42,7)\|PYROXENE RICH ORE(40,16)\|OLIVINE(36,34)\|COMMINUTING(36,6)\|COPPER FILING HEATED BED(34,4)\|THERMODYNAMIC EQUILIBRIUM(32,2)\|RESIDENCE RIME(32,1)\|PRESELECTED SIZE(31,13)\|ACIDIC SOLUTION(31,7)\|WATER OXYGEN FUGACITY(29,4)\|PYROXENE BEARING ORE(29,3)\|CARBON DIOXIDE(28,112)\|MINERAL ASSEMBLAGE(28,2)\|COMPLEX MINERALOGY(28,1)\|PYROXENE(27,20)\|SERPENTINIZATION REACTION(24,24)\|GAS SEPARATOR(22,11)\|AMBIENT TEMPERATURE(22,6)\|MAGNESIUM CARBONATE(20,39)\|CHROMIUM(19,9)\|MAGNETIC SEPARATOR(19,7)\|SUPERCRITICAL CARBON DIOXIDE(19,3)\|SCARCE METAL PRODUCTION(18,1)\|HYDROGEN GAS(17,50)\|COBALT(17,11)\|CARBON INTENSIVE(17,2)\|SCARCE METAL(16,16)\|CARBON DIOXIDE MINERALIZATION(16,5)\|PRODUCING MAGNETITE(16,4)\|HYDROGEN FORMATION(16,1)\|NATURAL GAS REFORMING(16,1)\|MAGNESITE(15,29)\|CRUSHER(14,5)\|FLUID COMMUNICATION(14,3)\|NATURAL GAS AVAILABILITY(14,1)\|VAIYING REACTION CONDITION(14,1)\|RESIDENCE TIME(12,37)\|SIEVE(12,9)\|ROCK POWDER(11,6)\|LITHIUM(11,3)\|CHEMISTRY(11,2)\|ATMOSPHERIC PRESSURE(10,8)\|PATHWAY(10,7)\|COMMINUTED ROCK(10,4)\|FORSTERITE MINERAL(10,4)\|IMMENSE GEOLOGICAL SCALABILITY(10,1)\|REACTION PRODUCT(9,22)\|INORGANIC PHASE(9,17)\|PRECIOUS METAL(9,7)\|OLIVINE RICH ORE(9,2)\|DESIRED MINERAL(9,1)\|RARE EARTH ELEMENT(8,12)\|CARBON SEQUESTRATION(8,9)\|CARBONIZATION REACTION(8,5)\|UNREACTED ROCK ORE(8,3)\|GANGUE MATERIAL(8,2)\|WEATHERED MINERAL MINING(8,1)\|YOUNG OCEANIC CMST(8,1)\|CRUSHED GROUND ROCK(7,6)\|WASHER(7,3)\|ECONOMIC VIABILITY(7,2)\|NEUTRALIZE ACIDIFICATION(7,2)\|FAYALITE PRECONCENTRATION(7,1)\|FAYALITE SERPENTINIZATION(7,1)\|MAFIC IGNEOUS ROCK POTENTIAL(7,1)\|MAFIC ULTRAMAFIC ORE(7,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(7,1)\|MINERAL GRAIN COMMINUTION(7,1)\|OLIVINE RICH DEPOSIT(7,1)\|SUPERCRITICAL CAIBON DIOXIDE(7,1)\|ACCESSORY MINERAL COLLECTION(6,3)\|THERMOCOUPLE DETECTOR(6,3)\|AGGREGATE SUBSTITUTE(6,2)\|FERROSILITE MINERAL PHASE(6,2)\|MAFIC IGNEOUS ROCK SOURCE(6,2)\|PULVERIZED ROCK(6,2)\|RESIDUAL GANGUE(6,2)\|UNREACTED ORE ROCK(6,2)\|CARBON MINERALIZATION KINETICS(6,1)\|GASEOUS CO2 DISSOLUTION(6,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(6,1)\|OLIVINE ABUNDANCE(6,1)\|ORE CARBONATION DRIVEN COMMINUTION(6,1)\|PYROXENE MINERALOGY(6,1)\|RELEVANT CONSTITUENT ABUNDANCE(6,1)\|REVENUE ENTITLEMENT(6,1)\|SEQUESTRATION TAX CREDIT(6,1)\|SERPENTINIZATION REACTION REACTIVITY(6,1)\|SERPENTINIZED ULTRAMAFIC ROCK(6,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(6,1)\|SMALL SIZE FRACTION(5,10)\|CARBON NEUTRAL(5,6)\|SRI GAS CHROMATOGRAPH(5,3)\|BAND HEATER(5,2)\|BATCH EXPERIMENT(5,2)\|CERAMIC BRICK(5,2)\|FRACTIONATION FACTOR(5,2)\|GEOLOGICAL SITE(5,2)\|MAGNETITE MAGNESITE PRODUCTION(5,2)\|PYROLYSIS REACTION(5,2)\|RELEVANT COMPONENT(5,2)\|REMAINING ROCK GANGUE(5,2)\|ROUGH PUMP(5,2)\|ABIOGENIC METHANE FORMATION(5,1)\|CARBON MINERALIZATION EXPERIMENT(5,1)\|COMMINUTED ORE(5,1)\|EARTH CONTINENTAL CRUST(5,1)\|ECONOMIC GEOLOGICAL HYDROGEN(5,1)\|FORSTERITE AVAILABILITY(5,1)\|GANGUE MINERAL(5,1)\|GASEOUS CAIBON REACTION(5,1)\|HOMOGENIZED OLIVINE(5,1)\|HYDROGEN EVOLUTION KINETICS(5,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(5,1)\|NONCONDENSABLE FRACTION(5,1)\|REMAINING BULK ROCK GEOCHEMICAL(5,1)\|ROCK ORE BREAKDOWN(5,1)\|SCALABLE MAGNESITE(5,1)\|SCIENTIFIC SUPPLIER(5,1)\|SEQUENTIAL CARBONIZATION(5,1)\|STEAM METHANE REFORMING REACTION(5,1)\|STOICHIOMETRIC ASSESSMENT(5,1)\|STOICHIOMETRIC MODELING(5,1)\|UNREACTED FAYALITE(5,1)\|YOUNG OCEANIC CRUST(5,1)\|REACTOR VESSEL(4,9)\|GRAVITY SEPARATION(4,8)\|FERTILIZER(4,4)\|PRESELECTED TEMPERATURE(4,4)\|STANDARD OMEGA(4,4)\|ACCOUNTING(4,3)\|DIHYDROGEN SULFIDE(4,3)\|ELECTRICITY(4,3)\|EVEN CARBON NEGATIVE(4,3)\|IRON RICH SILICATE MINERAL(4,3)\|LANDFILL(4,3)\|NATURAL REACTION(4,3)\|REMAINING ROCK ORE(4,3)\|ROTARY KILN(4,3)\|SEQUENTIAL REACTION(4,3)\|VALUABLE CONSTITUENT(4,3)\|COMPETITION(4,2)\|COPPER BED(4,2)\|OLIVINE WASTE STREAM(4,2)\|OMEGA K WIRE THERMOCOUPLE(4,2)\|RESIDUAL GAS ANALYZER(4,2)\|AGGREGATE SALE(4,1)\|AMBIENT OXYGEN FUGACITY(4,1)\|CARBONATE MINERALIZATION(4,1)\|COMMENSURATE LY(4,1)\|ENABLED EXPERIMENTATION(4,1)\|ENSTATITE MINERAL(4,1)\|GOVERNMENT MANDATED REGULATION(4,1)\|MAGNETITE RECOVERY(4,1)\|MID OCEANIC RIDGE(4,1)\|MINERAL BREAKDOWN(4,1)\|MITIGATE ATMOSPHERIC RELEASE(4,1)\|PROLIFIC OCCURRENCE(4,1)\|QUARRYING CONCEPT(4,1)\|REACTION SEQUENTIAL ORDERING(4,1)\|ROCK HAMMER(4,1)\|ROCK METRIC TON(4,1)\|SEQUENTIAL SERPENTINIZATION REACTION(4,1)\|STEAM REFORMER(4,1)\|STOICHIOMETRIC CALCULATION(4,1)\|THERMOCHEMICAL DRIVER(4,1)\|ULTRAMAFIC ROCK BULK SAMPLE(4,1)\|REACTION STEP(3,25)\|HEAVY LIQUID SEPARATION(3,5)\|SODIUM BICARBONATE(3,5)\|POTASSIUM HYDROXIDE(3,4)\|PSI PRESSURE GAUGE(3,4)\|ACCESSORY MINERAL PHASE(3,2)\|AGRICULTURAL LIME(3,2)\|BRUCITE(3,2)\|CARBON DIOXIDE INTRODUCTION(3,2)\|CRUSHING(3,2)\|ELECTROLYSIS(3,2)\|ENHANCING PRODUCTION(3,2)\|MAGNESIUM COMPONENT(3,2)\|MAGNETITE REACTION PRODUCT(3,2)\|METAL ENRICHMENT(3,2)\|SOURCE ROCK COMMINUTION(3,2)\|ULTRAMAFIC AGGREGATE MATERIAL(3,2)\|UNREACTED CARBON DIOXIDE(3,2)\|ACCESSORY OXIDE(3,1)\|ACTIVE QUARRY(3,1)\|ANTIGORITE REACTION(3,1)\|ASBESTOS BACK DEHYDRATION(3,1)\|BEST MECHANISTIC REACTION(3,1)\|BULK ORE(3,1)\|CARBON ECONOMY PURSUIT(3,1)\|CARBON MINERALIZATION KINETIC RATE(3,1)\|CARBON MINERALIZATION RATE(3,1)\|CARBON NEGATIVE CONCRETE FDLER(3,1)\|CARBON NEUTRAL PURSUIT(3,1)\|CARBON SEQUESTERING CARBONATION REACTION(3,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(3,1)\|CEMENT MANUFACTURING(3,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(3,1)\|CO2 OCCURRENCE(3,1)\|COMPETING REACTION OCCURRENCE(3,1)\|COMPLEX CHEMISTRY(3,1)\|CONCENTRATE SCARCE METAL(3,1)\|CONTAMINANT GAS(3,1)\|CRUSHED GROUND ORE(3,1)\|CRYOGENIC SEPARATION(3,1)\|DENSER IRON SILICATE(3,1)\|DERIVATIVE UTILIZATION(3,1)\|DESCRIPTIVE SENSE(3,1)\|DEVELOPMENT EFFORT(3,1)\|DISPOSITIONING(3,1)\|ELEVATED IRON CONTENT(3,1)\|ENHANCE KINETICS(3,1)\|ENHANCED MAGNETITE PRODUCTION(3,1)\|EXPERIMENTAL RUN(3,1)\|EXPLOIT GEOLOGICAL FORMATION(3,1)\|EXPLOITATION(3,1)\|EXTRACT HYDROGEN(3,1)\|FAYALITE HYDRATION REACTION(3,1)\|FC SBO(3,1)\|FC SFO(3,1)\|FLUID GEOCHEMISTRY(3,1)\|FLUID SAMPLING PORT(3,1)\|FORSTEIITE COMPONENT(3,1)\|FORSTERITE REACTION(3,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(3,1)\|GENERIC SENSE(3,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(3,1)\|GRAVITY SEPARATOR(3,1)\|GREEN AMMONIA(3,1)\|GREEN GOLDEN HYDROGEN(3,1)\|GROUNDWATER TREATMENT(3,1)\|HYDROGEN GENERATION COPRODUCT(3,1)\|IRON RICH IRON SILICA(3,1)\|IRON RICH MINERAL(3,1)\|IRON RICH OLIVINE(3,1)\|LABILE CARBON(3,1)\|MACHINERY PLACEMENT(3,1)\|MAGNESITE FORMATION(3,1)\|MAGNESITE GENERATION(3,1)\|MAGNESITE VALUE UTILIZATION(3,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(3,1)\|MAGNESIUM RICH SILICATE MINERAL(3,1)\|MAGNESIUM SILICATE CONVERSION(3,1)\|MAGNETITE PARTICLE(3,1)\|MAGNETITE REMOVAL(3,1)\|MAGNETITE YIELD(3,1)\|MEANINGFUL BENEFIT(3,1)\|METHANE CONVERSION(3,1)\|MG SIO(3,1)\|MIL NACL SALINE SOLUTION(3,1)\|MILDLY ACIDIC CONDITION(3,1)\|MILDLY ACIDIC SOLUTION(3,1)\|MINERAL PROCESSING(3,1)\|MINERAL SECONDARY RECOVERY(3,1)\|MINERAL SLAG(3,1)\|MUNICIPAL WASTEWATER TREATMENT(3,1)\|OLIVINE MINERAL PHASE(3,1)\|OLIVINE TEST(3,1)\|PHASE MINERAL UNITY(3,1)\|PREEVACUATED SAMPLE CHAMBER(3,1)\|PRIMARY DIFFERENTIATOR(3,1)\|PROCESSED ROCK(3,1)\|PYROXENE BEARING LOCALITY(3,1)\|REMAINING ROCK UNREACTED ORE(3,1)\|REMAINING UNREACTED ORE(3,1)\|RESIDUAL IRON SILICATE(3,1)\|RESIDUAL OLIVINE(3,1)\|ROBUST DEPOSIT(3,1)\|ROCK CONTENT(3,1)\|ROCK PREPARATION PHASE(3,1)\|SCARCE METAL RESOURCE(3,1)\|SEALED REACTOR(3,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(3,1)\|SERPENTINIZATION HYDRATION REACTION(3,1)\|SERPENTINIZATION REACTION KINETIC RATE(3,1)\|SERPENTINIZATION REACTION PHASE(3,1)\|SIO2 DENSITY SEPARATION(3,1)\|SOHD REACTION PRODUCT(3,1)\|SOLUTION GLOBAL APPLICABILITY(3,1)\|SPEX BALL MILL(3,1)\|SR QUADRUPOLE MASS SPECTROMETER(3,1)\|STANDARD GEOTHERMOMETER(3,1)\|STOICHIOMETRIC PROPORTION(3,1)\|STONE AGGREGATE FORMATION(3,1)\|TARGET PRODUCTION(3,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(3,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(3,1)\|ULTRAMAFIC FORMATION(3,1)\|UNDESIRED MINERAL SPECIES(3,1)\|UNIFORM SIZING(3,1)\|VARIABLE OXYGEN FUGACITY(3,1)\|VISIBLE OLIVINE(3,1)\|WATER LOWERED OXYGEN FUGACITY(3,1)\|MAGNESIUM OXIDE(2,4)\|STOICHIOMETRIC RATIO(2,4)\|CARBON DIOXIDE GAS(2,3)\|FACILITY(2,3)\|FLUIDIZED BED(2,3)\|GRINDER(2,3)\|HYDROGEN GAS EVOLUTION(2,3)\|IRON SILICATE PHASE(2,3)\|PRELIMINARY RESULT(2,3)\|SULFUR DIOXIDE(2,3)\|FLOWCHART BLOCK(2,2)\|FOSSIL FUEL COMBUSTION(2,2)\|ABIOTIC HYDROGEN PRODUCTION(2,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(2,1)\|ALUMINOSILICATE(2,1)\|AMPLIFICATION(2,1)\|ATMOSPHERIC CONDITION(2,1)\|ATTRACTION(2,1)\|CARBON DIOXIDE EMISSION(2,1)\|CARBON DIOXIDE PURITY(2,1)\|CARBON DIOXIDE REACTIVITY(2,1)\|CARBON NEGATIVE CONCRETE FILLER(2,1)\|CARBON SEQUESTRATION CAPACITY(2,1)\|CRASHER(2,1)\|DECADE(2,1)\|ENHANCING CARBON DIOXIDE(2,1)\|EXPANSION VOLUME(2,1)\|FINE POWDER(2,1)\|FLUID CHEMISTRY(2,1)\|GEOLOGICAL SOURCE(2,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(2,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(2,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(2,1)\|INCREASED MINERALIZATION(2,1)\|INCREASED REACTIVITY(2,1)\|INORGANIC PRODUCT(2,1)\|INTENDED CARBONATION REACTION(2,1)\|REACHING RESERVE(2,1)\|\|(AU2022318480)\|REACTOR(100,174)\|MAGNETITE(100,64)\|ROCK(100,34)\|HYDROGEN(100,26)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,8)\|HYDROGEN GENERATION(100,7)\|ORE(69,64)\|REMAINING ORE(69,31)\|ORE PARTICLE(57,11)\|MAGNESITE SEQUENTIAL CARBONATION(53,1)\|MAFIC IGNEOUS ROCK(45,7)\|ROCK ASSEMBLAGE(43,1)\|ULTRAMAFIC IGNEOUS ROCK(42,7)\|PYROXENE RICH ORE(41,16)\|OLIVINE(36,34)\|COMMINUTING(36,6)\|COPPER FILING HEATED BED(34,4)\|THERMODYNAMIC EQUILIBRIUM(32,2)\|PRESELECTED SIZE(31,13)\|ACIDIC SOLUTION(31,7)\|WATER OXYGEN FUGACITY(29,4)\|CARBON DIOXIDE(28,114)\|PYROXENE BEARING ORE(28,3)\|MINERAL ASSEMBLAGE(28,2)\|COMPLEX MINERALOGY(28,1)\|PYROXENE(27,20)\|SERPENTINIZATION REACTION(24,24)\|GAS SEPARATOR(22,11)\|AMBIENT TEMPERATURE(22,6)\|MAGNESIUM CARBONATE(20,39)\|CHROMIUM(19,9)\|MAGNETIC SEPARATOR(19,7)\|SUPERCRITICAL CARBON DIOXIDE(18,4)\|SCARCE METAL PRODUCTION(18,1)\|HYDROGEN GAS(17,50)\|COBALT(17,11)\|CARBON INTENSIVE(17,2)\|SCARCE METAL(16,16)\|CARBON DIOXIDE MINERALIZATION(16,5)\|PRODUCING MAGNETITE(16,4)\|HYDROGEN FORMATION(16,1)\|NATURAL GAS REFORMING(16,1)\|MAGNESITE(15,29)\|CRUSHER(14,6)\|FLUID COMMUNICATION(14,3)\|NATURAL GAS AVAILABILITY(14,1)\|OLIVINE PYROXENE SERPENTINE FORSTERITE(14,1)\|RESIDENCE TIME(12,38)\|SIEVE(12,9)\|ROCK POWDER(11,6)\|LITHIUM(11,3)\|CHEMISTRY(11,2)\|ATMOSPHERIC PRESSURE(10,8)\|PATHWAY(10,7)\|COMMINUTED ROCK(10,4)\|FORSTERITE MINERAL(10,4)\|IMMENSE GEOLOGICAL SCALABILITY(10,1)\|MAFIC ROCK REACHING RESERVE(10,1)\|REACTION PRODUCT(9,22)\|INORGANIC PHASE(9,17)\|PRECIOUS METAL(9,7)\|OLIVINE RICH ORE(9,2)\|DESIRED MINERAL(9,1)\|RARE EARTH ELEMENT(8,12)\|CARBON SEQUESTRATION(8,9)\|CARBONIZATION REACTION(8,5)\|UNREACTED ROCK ORE(8,3)\|GANGUE MATERIAL(8,2)\|WEATHERED MINERAL MINING(8,1)\|CRUSHED GROUND ROCK(7,6)\|WASHER(7,3)\|ECONOMIC VIABILITY(7,2)\|NEUTRALIZE ACIDIFICATION(7,2)\|YOUNG OCEANIC CRUST(7,2)\|FAYALITE PRECONCENTRATION(7,1)\|FAYALITE SERPENTINIZATION(7,1)\|MAFIC IGNEOUS ROCK POTENTIAL(7,1)\|MAFIC ULTRAMAFIC ORE(7,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(7,1)\|MINERAL GRAIN COMMINUTION(7,1)\|OLIVINE RICH DEPOSIT(7,1)\|ACCESSORY MINERAL COLLECTION(6,3)\|THERMOCOUPLE DETECTOR(6,3)\|AGGREGATE SUBSTITUTE(6,2)\|FERROSILITE MINERAL PHASE(6,2)\|MAFIC IGNEOUS ROCK SOURCE(6,2)\|PULVERIZED ROCK(6,2)\|RESIDUAL GANGUE(6,2)\|UNREACTED ORE ROCK(6,2)\|CARBON MINERALIZATION KINETICS(6,1)\|GASEOUS CO2 DISSOLUTION(6,1)\|IGNEOUS MINERAL CO2(6,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(6,1)\|OLIVINE ABUNDANCE(6,1)\|ORE CARBONATION DRIVEN COMMINUTION(6,1)\|PYROXENE MINERALOGY(6,1)\|RELEVANT CONSTITUENT ABUNDANCE(6,1)\|REVENUE ENTITLEMENT(6,1)\|SEQUESTRATION TAX CREDIT(6,1)\|SERPENTINIZATION REACTION REACTIVITY(6,1)\|SERPENTINIZED ULTRAMAFIC ROCK(6,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(6,1)\|SMALL SIZE FRACTION(5,10)\|CARBON NEUTRAL(5,6)\|COPPER BED(5,3)\|SRI GAS CHROMATOGRAPH(5,3)\|BAND HEATER(5,2)\|BATCH EXPERIMENT(5,2)\|CERAMIC BRICK(5,2)\|CO2 MINERALIZATION RATE(5,2)\|FRACTIONATION FACTOR(5,2)\|GEOLOGICAL SITE(5,2)\|MAGNETITE MAGNESITE PRODUCTION(5,2)\|PYROLYSIS REACTION(5,2)\|RELEVANT COMPONENT(5,2)\|ROUGH PUMP(5,2)\|ABIOGENIC METHANE FORMATION(5,1)\|CARBON MINERALIZATION EXPERIMENT(5,1)\|COMMINUTED ORE(5,1)\|EARTH CONTINENTAL CRUST(5,1)\|ECONOMIC GEOLOGICAL HYDROGEN(5,1)\|FORSTERITE AVAILABILITY(5,1)\|GANGUE MINERAL(5,1)\|HOMOGENIZED OLIVINE(5,1)\|HYDROGEN EVOLUTION KINETICS(5,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(5,1)\|NONCONDENSABLE FRACTION(5,1)\|REMAINING BULK ROCK GEOCHEMICAL(5,1)\|ROCK ORE BREAKDOWN(5,1)\|SCALABLE MAGNESITE(5,1)\|SCIENTIFIC SUPPLIER(5,1)\|SEQUENTIAL CARBONIZATION(5,1)\|STEAM METHANE REFORMING REACTION(5,1)\|STOICHIOMETRIC ASSESSMENT(5,1)\|STOICHIOMETRIC MODELING(5,1)\|ULTMMAFIC ROCK(5,1)\|UNREACTED FAYALITE(5,1)\|REACTOR VESSEL(4,9)\|GRAVITY SEPARATION(4,8)\|REACTION CONDITION(4,6)\|CRUSHING(4,4)\|FERTILIZER(4,4)\|PRESELECTED TEMPERATURE(4,4)\|STANDARD OMEGA(4,4)\|ACCOUNTING(4,3)\|DIHYDROGEN SULFIDE(4,3)\|ELECTRICITY(4,3)\|EVEN CARBON NEGATIVE(4,3)\|IRON RICH SILICATE MINERAL(4,3)\|LANDFILL(4,3)\|NATURAL REACTION(4,3)\|REMAINING ROCK ORE(4,3)\|SEQUENTIAL REACTION(4,3)\|VALUABLE CONSTITUENT(4,3)\|COMPETITION(4,2)\|OLIVINE WASTE STREAM(4,2)\|OMEGA K WIRE THERMOCOUPLE(4,2)\|REMAINING ROCK GANGUE(4,2)\|RESIDUAL GAS ANALYZER(4,2)\|SUPERCRITICAL CO2(4,2)\|AGGREGATE SALE(4,1)\|AMBIENT OXYGEN FUGACITY(4,1)\|CARBONATE MINERALIZATION(4,1)\|ENABLED EXPERIMENTATION(4,1)\|ENSTATITE MINERAL(4,1)\|GOVERNMENT MANDATED REGULATION(4,1)\|MAGNETITE RECOVERY(4,1)\|MID OCEANIC RIDGE(4,1)\|MINERAL BREAKDOWN(4,1)\|MITIGATE ATMOSPHERIC RELEASE(4,1)\|PROLIFIC OCCURRENCE(4,1)\|QUARRYING CONCEPT(4,1)\|REACTION SEQUENTIAL ORDERING(4,1)\|ROCK HAMMER(4,1)\|ROCK METRIC TON(4,1)\|SEQUENTIAL SERPENTINIZATION REACTION(4,1)\|STEAM REFORMER(4,1)\|STOICHIOMETRIC CALCULATION(4,1)\|THERMOCHEMICAL DRIVER(4,1)\|ULTRAMAFIC ROCK BULK SAMPLE(4,1)\|REACTION STEP(3,24)\|HEAVY LIQUID SEPARATION(3,5)\|MGCO3(3,5)\|SODIUM BICARBONATE(3,5)\|POTASSIUM HYDROXIDE(3,4)\|PSI PRESSURE GAUGE(3,4)\|ACCESSORY MINERAL PHASE(3,2)\|AGRICULTURAL LIME(3,2)\|BRUCITE(3,2)\|CARBON DIOXIDE INTRODUCTION(3,2)\|CARBON NEGATIVE CONCRETE FILLER(3,2)\|ELECTROLYSIS(3,2)\|ENHANCING PRODUCTION(3,2)\|FE2SIO(3,2)\|MAGNESIUM COMPONENT(3,2)\|MAGNETITE REACTION PRODUCT(3,2)\|METAL ENRICHMENT(3,2)\|MG2SIO(3,2)\|SOURCE ROCK COMMINUTION(3,2)\|ULTRAMAFIC AGGREGATE MATERIAL(3,2)\|UNREACTED CARBON DIOXIDE(3,2)\|ACCESSORY OXIDE(3,1)\|ACTIVE QUARRY(3,1)\|ANTIGORITE REACTION(3,1)\|ASBESTOS BACK DEHYDRATION(3,1)\|BEST MECHANISTIC REACTION(3,1)\|BULK ORE(3,1)\|CARBON ECONOMY PURSUIT(3,1)\|CARBON MINERALIZATION KINETIC RATE(3,1)\|CARBON MINERALIZATION RATE(3,1)\|CARBON NEUTRAL PURSUIT(3,1)\|CARBON SEQUESTERING CARBONATION REACTION(3,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(3,1)\|CEMENT MANUFACTURING(3,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(3,1)\|CIRCUMNEUTRAL PH(3,1)\|CO2 OCCURRENCE(3,1)\|CO2 REDUCTION(3,1)\|COMPETING REACTION OCCURRENCE(3,1)\|COMPLEX CHEMISTRY(3,1)\|CONCENTRATE SCARCE METAL(3,1)\|CONTAMINANT GAS(3,1)\|CRUSHED GROUND ORE(3,1)\|CRYOGENIC SEPARATION(3,1)\|DENSER IRON SILICATE(3,1)\|DERIVATIVE UTILIZATION(3,1)\|DESCRIPTIVE SENSE(3,1)\|DEVELOPMENT EFFORT(3,1)\|DISPOSITIONING(3,1)\|ELEVATED IRON CONTENT(3,1)\|ENHANCE KINETICS(3,1)\|ENHANCED MAGNETITE PRODUCTION(3,1)\|EXPERIMENTAL RUN(3,1)\|EXPLOIT GEOLOGICAL FORMATION(3,1)\|EXPLOITATION(3,1)\|EXTRACT HYDROGEN(3,1)\|FAYALITE HYDRATION REACTION(3,1)\|FLUID GEOCHEMISTRY(3,1)\|FLUID SAMPLING PORT(3,1)\|FORSTERITE COMPONENT(3,1)\|FORSTERITE REACTION(3,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(3,1)\|GENERIC SENSE(3,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(3,1)\|GRAVITY SEPARATOR(3,1)\|GREEN AMMONIA(3,1)\|GREEN GOLDEN HYDROGEN(3,1)\|GROUNDWATER TREATMENT(3,1)\|HYDROGEN GENERATION COPRODUCT(3,1)\|IRON RICH IRON SILICA(3,1)\|IRON RICH MINERAL(3,1)\|IRON RICH OLIVINE(3,1)\|LABILE CARBON(3,1)\|MACHINERY PLACEMENT(3,1)\|MAGNESITE FORMATION(3,1)\|MAGNESITE GENERATION(3,1)\|MAGNESITE VALUE UTILIZATION(3,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(3,1)\|MAGNESIUM RICH SILICATE MINERAL(3,1)\|MAGNESIUM SILICATE CONVERSION(3,1)\|MAGNETITE PARTICLE(3,1)\|MAGNETITE REMOVAL(3,1)\|MAGNETITE YIELD(3,1)\|MEANINGFUL BENEFIT(3,1)\|METHANE CONVERSION(3,1)\|MIL NACL SALINE SOLUTION(3,1)\|MILDLY ACIDIC CONDITION(3,1)\|MILDLY ACIDIC SOLUTION(3,1)\|MINERAL PROCESSING(3,1)\|MINERAL SECONDARY RECOVERY(3,1)\|MINERAL SLAG(3,1)\|MUNICIPAL WASTEWATER TREATMENT(3,1)\|OLIVINE MINERAL PHASE(3,1)\|OLIVINE TEST(3,1)\|PH AMENDMENT(3,1)\|PHASE DECARBONATION REACTION MOLE(3,1)\|PHASE MINERAL UNITY(3,1)\|PREEVACUATED SAMPLE CHAMBER(3,1)\|PRIMARY DIFFERENTIATOR(3,1)\|PROCESSED ROCK(3,1)\|PURITY CO2(3,1)\|PYROXENE BEARING LOCALITY(3,1)\|REMAINING ROCK UNREACTED ORE(3,1)\|REMAINING UNREACTED ORE(3,1)\|RESIDUAL IRON SILICATE(3,1)\|RESIDUAL OLIVINE(3,1)\|ROBUST DEPOSIT(3,1)\|ROCK CONTENT(3,1)\|ROCK PREPARATION PHASE(3,1)\|SCARCE METAL RESOURCE(3,1)\|SEALED REACTOR(3,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(3,1)\|SERPENTINIZATION REACTION KINETIC RATE(3,1)\|SERPENTINIZATION REACTION PHASE(3,1)\|SIO2 DENSITY SEPARATION(3,1)\|SOLUTION GLOBAL APPLICABILITY(3,1)\|SPEX BALL MILL(3,1)\|SR QUADRUPOLE MASS SPECTROMETER(3,1)\|STANDARD GEOTHERMOMETER(3,1)\|STOICHIOMETRIC PROPORTION(3,1)\|STONE AGGREGATE FORMATION(3,1)\|TARGET PRODUCTION(3,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(3,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(3,1)\|ULTRAMAFIC FORMATION(3,1)\|UNDESIRED MINERAL SPECIES(3,1)\|UNIFORM SIZING(3,1)\|VARIABLE OXYGEN FUGACITY(3,1)\|VISIBLE OLIVINE(3,1)\|WATER LOWERED OXYGEN FUGACITY(3,1)\|MAGNESIUM OXIDE(2,4)\|STOICHIOMETRIC RATIO(2,4)\|CARBON DIOXIDE GAS(2,3)\|FACILITY(2,3)\|FLUIDIZED BED(2,3)\|GRINDER(2,3)\|HYDROGEN GAS EVOLUTION(2,3)\|IRON SILICATE PHASE(2,3)\|PRELIMINARY RESULT(2,3)\|ROTARY KILN(2,3)\|SO2(2,3)\|SULFUR DIOXIDE(2,3)\|FLOWCHART BLOCK(2,2)\|FOSSIL FUEL COMBUSTION(2,2)\|STAINLESS STEEL REACTION VESSEL(2,2)\|ABIOTIC HYDROGEN PRODUCTION(2,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(2,1)\|ALUMINOSILICATE(2,1)\|AMPLIFICATION(2,1)\|ATMOSPHERIC CONDITION(2,1)\|ATTRACTION(2,1)\|BATCH CONDITION(2,1)\|CARBON DIOXIDE EMISSION(2,1)\|CARBON DIOXIDE PURITY(2,1)\|CARBON DIOXIDE REACTIVITY(2,1)\|CARBON SEQUESTRATION CAPACITY(2,1)\|CO2 ELEVATED PRESSURE(2,1)\|CO2 RATIO(2,1)\|DECADE(2,1)\|ENHANCING CARBON DIOXIDE(2,1)\|EXPANSION VOLUME(2,1)\|FINE POWDER(2,1)\|FLUID CHEMISTRY(2,1)\|GEOLOGICAL SOURCE(2,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(2,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(2,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(2,1)\|INCREASED MINERALIZATION(2,1)\|INCREASED REACTIVITY(2,1)\|INORGANIC PRODUCT(2,1)\|INTENDED CARBONATION REACTION(2,1)\|IRON ORE NATURE(2,1)\|\|(CA3227505)\|REACTOR(100,130)\|MAGNETITE(100,60)\|ROCK(100,32)\|HYDROGEN(100,26)\|HYDROGEN PRODUCTION(100,13)\|SEQUESTERING CARBON(100,7)\|HYDROGEN GENERATION(100,6)\|YAWING MINERAL ASSEMBLAGE(84,1)\|ORE(80,48)\|YAWING MINERAL ASSEMBLAGE COMPLEX(76,1)\|REMAINING ORE(67,20)\|ROCK ASSEMBLAGE(62,1)\|NAMIC EQUILIBRIUM(55,1)\|PYROXENE RICH ORE(50,15)\|OLIVINE(49,33)\|MAFIC IGNEOUS ROCK(48,6)\|PYROXENE BEARING ORE(47,2)\|ULTRAMAFIC IGNEOUS ROCK(45,6)\|ORE PARTICLE(43,5)\|COMMINUTING(42,3)\|PYROXENE(40,20)\|COMPLEX MINERALOGY(40,1)\|SERPENTINIZATION REACTION(34,22)\|GAS SEPARATOR(32,11)\|AMBIENT TEMPERATURE(32,6)\|SCARCE METAL PRODUCTION(27,1)\|COPPER FILING HEATED BED(26,2)\|CARBON DIOXIDE(25,92)\|MAGNESIUM CARBONATE(25,37)\|HYDROGEN GAS(24,49)\|CARBON INTENSIVE(24,2)\|CARBON DIOXIDE MINERALIZATION(23,5)\|PRODUCING MAGNETITE(23,4)\|HYDROGEN FORMATION(23,1)\|NATURAL GAS REFORMING(23,1)\|MAGNESITE(22,28)\|WATER OXYGEN FUGACITY(22,2)\|PRESELECTED SIZE(21,5)\|FLUID COMMUNICATION(21,3)\|NATURAL GAS AVAILABILITY(21,1)\|OLIVINE PYROXENE SERPENTINE FORSTERITE(21,1)\|SCARCE METAL(19,15)\|SUPERCRITICAL CARBON DIOXIDE(18,3)\|ROCK POWDER(17,6)\|CHEMISTRY(16,2)\|ATMOSPHERIC PRESSURE(15,8)\|FORSTERITE MINERAL(15,4)\|INORGANIC PHASE(14,17)\|PATHWAY(14,7)\|COMMINUTED ROCK(14,4)\|SEQUENTIAL CARBONATION(14,4)\|OLIVINE RICH ORE(14,2)\|IMMENSE GEOLOGICAL SCALABILITY(14,1)\|REACTION PRODUCT(13,22)\|DESIRED MINERAL(13,1)\|RESIDENCE TIME(12,22)\|CARBON SEQUESTRATION(12,9)\|CARBONIZATION REACTION(12,5)\|WEATHERED MINERAL MINING(12,1)\|CRUSHED GROUND ROCK(11,6)\|UNREACTED ROCK ORE(11,3)\|LITHIUM(11,2)\|NEUTRALIZE ACIDIFICATION(11,2)\|YOUNG OCEANIC CRUST(11,2)\|FAYALITE PRECONCENTRATION(11,1)\|FAYALITE SERPENTINIZATION(11,1)\|COBALT(10,7)\|CHROMIUM(10,5)\|MAGNETIC SEPARATOR(10,5)\|ECONOMIC VIABILITY(10,2)\|MAFIC IGNEOUS ROCK POTENTIAL(10,1)\|MAFIC ULTRAMAFIC ORE(10,1)\|MAGNETITE GENERATION THERMODYNAMIC DRIVER(10,1)\|MINERAL GRAIN COMMINUTION(10,1)\|OLIVINE RICH DEPOSIT(10,1)\|ACCESSORY MINERAL COLLECTION(9,3)\|THERMOCOUPLE DETECTOR(9,3)\|AGGREGATE SUBSTITUTE(9,2)\|FERROSILITE MINERAL PHASE(9,2)\|MAFIC IGNEOUS ROCK SOURCE(9,2)\|PULVERIZED ROCK(9,2)\|RESIDUAL GANGUE(9,2)\|CARBON MINERALIZATION KINETICS(9,1)\|GASEOUS CO2 DISSOLUTION(9,1)\|IGNEOUS MINERAL CO2(9,1)\|IMPOSED PRIVATE SECTOR INITIATIVE(9,1)\|OLIVINE ABUNDANCE(9,1)\|ORE CARBONATION DRIVEN COMMINUTION(9,1)\|PYROXENE MINERALOGY(9,1)\|RELEVANT CONSTITUENT ABUNDANCE(9,1)\|REVENUE ENTITLEMENT(9,1)\|SEQUESTRATION TAX CREDIT(9,1)\|SERPENTINIZATION REACTION REACTIVITY(9,1)\|SERPENTITHZED ULTRAMAFIC ROCK(9,1)\|STOICHIOMCTRIC ASSESSMENT(9,1)\|STOICHIOMETRIC SERPENTINIZATION REACTION(9,1)\|SIEVE(8,7)\|CARBON NEUTRAL(8,6)\|BAND HEATER(8,2)\|BATCH EXPERIMENT(8,2)\|CERAMIC BRICK(8,2)\|CO2 MINERALIZATION RATE(8,2)\|FRACTIONATION FACTOR(8,2)\|GEOLOGICAL SITE(8,2)\|MAGNETITE MAGNESITE PRODUCTION(8,2)\|RELEVANT COMPONENT(8,2)\|ROUGH PUMP(8,2)\|UNREACTED ORE ROCK(8,2)\|COPPER BED(7,3)\|RESIDUAL GAS ANALYZER(7,3)\|SRI GAS CHROMATOGRAPH(7,3)\|SUPERCRITICAL CO2(7,2)\|ABIOGENIC METHANE FORMATION(7,1)\|CARBON MINERALIZATION EXPERIMENT(7,1)\|COMMINUTED ORE(7,1)\|EARTH CONTINENTAL CRUST(7,1)\|FORSTERITE AVAILABILITY(7,1)\|GANGUE MINERAL(7,1)\|GREEN TECLMOLOGY(7,1)\|HOMOGENIZED OLIVINE(7,1)\|HYDROGEN EVOLUTION KINETICS(7,1)\|MAGNESITE MINERAL PHASE PRECIPITATION(7,1)\|NONCONDENSABLE FRACTION(7,1)\|PY ROLYSIS REACTION(7,1)\|REMAINING BULK ROCK GEOCHEMICAL(7,1)\|ROCK ORE BREAKDOWN(7,1)\|SCALABLE MAGNESITE(7,1)\|SCIENTIFIC SUPPLIER(7,1)\|SEQUENTIAL CARBONIZATION(7,1)\|STEAM METHANE REFORMING REACTION(7,1)\|STOICHIOMETRIC MODELING(7,1)\|STOICLIIOMETRIC CALCULATION(7,1)\|THERMODYNAMIC EQUILIBRIUM(7,1)\|UNREACTED FAYALITE(7,1)\|REACTOR VESSEL(6,9)\|GRAVITY SEPARATION(6,8)\|REACTION CONDITION(6,6)\|CRUSHER(6,4)\|CRUSHING(6,4)\|FERTILIZER(6,4)\|PRESELECTED TEMPERATURE(6,4)\|STANDARD OMEGA(6,4)\|SEQUENTIAL REACTION(6,3)\|COMPETITION(6,2)\|OLIVINE WASTE STREAM(6,2)\|OMEGA K WIRE THERMOCOUPLE(6,2)\|REMAINING ROCK GANGUE(6,2)\|AGGREGATE SALE(6,1)\|AMBIENT OXYGEN FUGACITY(6,1)\|CARBONATE MINERALIZATION(6,1)\|DECARBONATION REACTION MOLE(6,1)\|ENABLED EXPERIMENTATION(6,1)\|ENSTATITE MINERAL(6,1)\|GOVERNMENT MANDATED REGULATION(6,1)\|IRON OXIDELMAGNETITE(6,1)\|MAGNETITE RECOVERY(6,1)\|MID OCEANIC RIDGE(6,1)\|MINERAL ASSEMBLAGE(6,1)\|MINERAL BREAKDOWN(6,1)\|MITIGATE ATMOSPHERIC RELEASE(6,1)\|PROLIFIC OCCURRENCE(6,1)\|QUARRYING CONCEPT(6,1)\|REACHING RESERVE(6,1)\|REACTION SEQUENTIAL ORDERING(6,1)\|ROCK HAMMER(6,1)\|ROCK METRIC TON(6,1)\|SEQUENTIAL SERPENTINIZATION REACTION(6,1)\|STEAM REFORMER(6,1)\|THERMOCHEMICAL DRIVER(6,1)\|ULTRAMAFIC ROCK BULK SAMPLE(6,1)\|RARE EARTH ELEMENT(5,8)\|SMALL SIZE FRACTION(5,7)\|MGCO3(5,6)\|PRECIOUS METAL(5,6)\|HEAVY LIQUID SEPARATION(5,5)\|SODIUM BICARBONATE(5,5)\|ACCOUNTING(5,3)\|DIHYDROGEN SULFIDE(5,3)\|ELECTRICITY(5,3)\|EVEN CARBON NEGATIVE(5,3)\|IRON RICH SILICATE MINERAL(5,3)\|LANDFILL(5,3)\|MG2SIO(5,3)\|NATURAL REACTION(5,3)\|REMAINING ROCK ORE(5,3)\|VALUABLE CONSTITUENT(5,3)\|MAGNETITE REACTION PRODUCT(5,2)\|ANTIGORITE REACTION(5,1)\|BULK ORE(5,1)\|CARBON ECONOMY PURSUIT(5,1)\|CARBON MINERALIZATION KINETIC RATE(5,1)\|CARBON SEQUESTERING CARBONATION REACTION(5,1)\|CIRCUMNCUTRAL PH(5,1)\|CO2 OCCURRENCE(5,1)\|COMPETING REACTION OCCURRENCE(5,1)\|CONCENTRATE SCARCE METAL(5,1)\|CRYOGENIC SEPARATION(5,1)\|DENSER IRON SILICATE(5,1)\|DERIVATIVE UTILIZATION(5,1)\|ELEVATED IMN CONTENT(5,1)\|ENHANCE KINETICS(5,1)\|ENHANCED MAGNETITE PRODUCTION(5,1)\|EXPLOIT GEOLOGICAL FORMATION(5,1)\|FAYALITE HYDRATION REACTION(5,1)\|FLUID GEOCHEMISTRY(5,1)\|FORSTERITE REACTION(5,1)\|GASEOUS CARBON DIOXIDE SEQUESTRATION(5,1)\|GENERIC SENSE(5,1)\|GEOLOGICAL HYDROGEN(5,1)\|GRAVITY SEPARATOR(5,1)\|GROUNDWATER TREATMENT(5,1)\|IRON RICH CNDMCMBCR(5,1)\|IRON RICH OLIVINE(5,1)\|MACHINERY PLACEMENT(5,1)\|MAGNESITE FORMATION(5,1)\|MAGNESITE GENERATION(5,1)\|MAGNESIUM CARBONATE MINERAL LATTICE(5,1)\|MAGNETITE PARTICLE(5,1)\|MAGNETITE YIELD(5,1)\|MEANINGFUL BENEFIT(5,1)\|MILDLY ACIDIC CONDITION(5,1)\|MILDLY ACIDIC SOLUTION(5,1)\|MINERAL SLAG(5,1)\|MUNICIPAL WASTEWATER TREATMENT(5,1)\|OLIVINE MINERAL PHASE(5,1)\|PH AMENDMENT(5,1)\|PHASE MINERAL UNITY(5,1)\|PREEVACUATED SAMPLE CHAMBER(5,1)\|PRIMARY DIFFERENTIATOR(5,1)\|PURITY CO2(5,1)\|PYROLYSIS REACTION(5,1)\|PYROXENE BEARING LOCALITY(5,1)\|REMAINING ROCK UNREACTED ORE(5,1)\|REMAINING UNREACTED ORE(5,1)\|RESIDUAL OLIVINE(5,1)\|ROBUST DEPOSIT(5,1)\|SEMENTINIZATION REACTION(5,1)\|SERPCNTINIZATION REACTION(5,1)\|SERPENTINIZATION REACTION KINETIC RATE(5,1)\|SOLUTION GLOBAL APPLICABILITY(5,1)\|SPEX BALL MILL(5,1)\|STOICHIOMETRIC PROPORTION(5,1)\|STONE AGGREGATE FORMATION(5,1)\|THC ROCK(5,1)\|TOTAL CARBON MINERALIZATION ABUNDANCE(5,1)\|TROXENE BEARING ORE(5,1)\|ULTRAHIGH PURITY CARBON DIOXIDE(5,1)\|VARIABLE OXYGEN FUGACITY(5,1)\|VISIBLE OLIVINE(5,1)\|REACTION STEP(4,24)\|POTASSIUM HYDROXIDE(4,4)\|PSI PRESSURE GAUGE(4,4)\|ACCESSORY MINERAL PHASE(4,2)\|AGRICULTURAL LIME(4,2)\|CARBON DIOXIDE INTRODUCTION(4,2)\|CARBON NEGATIVE CONCRETE FILLER(4,2)\|ELECTROLYSIS(4,2)\|ENHANCING PRODUCTION(4,2)\|FE2SIO(4,2)\|FLOWCHART BLOCK(4,2)\|FOSSIL FUEL COMBUSTION(4,2)\|MAGNESIUM COMPONENT(4,2)\|METAL ENRICHMENT(4,2)\|SOURCE ROCK COMMINUTION(4,2)\|STAINLESS STEEL REACTION VESSEL(4,2)\|ULTRAMAFIC AGGREGATE MATERIAL(4,2)\|UNREACTED CARBON DIOXIDE(4,2)\|ACCESSORY OXIDE(4,1)\|ACTIVE QUARRY(4,1)\|ASBESTOS BACK DEHYDRATION(4,1)\|BEST MECHANISTIC REACTION(4,1)\|CARBON MINERALIZATION RATE(4,1)\|CARBON NEUTRAL PURSUIT(4,1)\|CARBONATION SERPENTINIZATION REACTION PRODUCT(4,1)\|CEMENT MANUFACTURING(4,1)\|CHEMICAL SPECIES TARGETED PRODUCTION(4,1)\|CO2 REDUCTION(4,1)\|COMPLEX CHEMISTRY(4,1)\|CONTAMINANT GAS(4,1)\|CRUSHED GROUND ORE(4,1)\|DESCRIPTIVE SENSE(4,1)\|DEVELOPMENT EFFORT(4,1)\|DISPOSITIONING(4,1)\|EXPERIMENTAL RUN(4,1)\|EXPLOITATION(4,1)\|EXTRACT HYDROGEN(4,1)\|FLUID SAMPLING PORT(4,1)\|FORSTERITE COMPONENT(4,1)\|GIVE REPRESENTATIVE CARBONATION REACTION(4,1)\|GREEN AMMONIA(4,1)\|GREEN GOLDEN HYDROGEN(4,1)\|HYDROGEN GENERATION COPRODUCT(4,1)\|IRON RICH IRON SILICA(4,1)\|IRON RICH MINERAL(4,1)\|LABILE CARBON(4,1)\|MAGNESITE VALUE UTILIZATION(4,1)\|MAGNESIUM RICH SILICATE MINERAL(4,1)\|MAGNESIUM SILICATE CONVERSION(4,1)\|MAGNETITE REMOVAL(4,1)\|METHANE CONVERSION(4,1)\|MINERAL PROCESSING(4,1)\|MINERAL SECONDARY RECOVERY(4,1)\|OLIVINE TEST(4,1)\|PROCESSED ROCK(4,1)\|RESIDUAL IRON SILICATE(4,1)\|ROCK CONTENT(4,1)\|ROCK PREPARATION PHASE(4,1)\|SCARCE METAL RESOURCE(4,1)\|SEALED REACTOR(4,1)\|SEPARATABLE MAGNETIC COMPONENT MASS(4,1)\|SERPENTINIZATION REACTION PHASE(4,1)\|SIO2 DENSITY SEPARATION(4,1)\|SR QUADRUPOLE MASS SPECTROMETER(4,1)\|STANDARD GEOTHERMOMETER(4,1)\|TARGET PRODUCTION(4,1)\|ULTRAMAFIC FORMATION(4,1)\|UNDESIRED MINERAL SPECIES(4,1)\|UNIFORM SIZING(4,1)\|WATER LOWERED OXYGEN FUGACITY(4,1)\|MAGNESIUM OXIDE(3,4)\|STOICHIOMETRIC RATIO(3,4)\|CARBON DIOXIDE GAS(3,3)\|FACILITY(3,3)\|FLUIDIZED BED(3,3)\|GRINDER(3,3)\|HYDROGEN GAS EVOLUTION(3,3)\|IRON SILICATE PHASE(3,3)\|PRELIMINARY RESULT(3,3)\|ROTARY KILN(3,3)\|SO2(3,3)\|SULFUR DIOXIDE(3,3)\|ABIOTIC HYDROGEN PRODUCTION(3,1)\|ACCESSORY COMPETITIVE PHASE FORMATION(3,1)\|ALUMINOSILICATE(3,1)\|AMPLIFICATION(3,1)\|ATMOSPHERIC CONDITION(3,1)\|ATTRACTION(3,1)\|BATCH CONDITION(3,1)\|BMCITE(3,1)\|BRUCITE(3,1)\|CARBON DIOXIDE EMISSION(3,1)\|CARBON DIOXIDE PURITY(3,1)\|CARBON DIOXIDE REACTIVITY(3,1)\|CARBON SEQUESTRATION CAPACITY(3,1)\|CO2 ELEVATED PRESSURE(3,1)\|CO2 RATIO(3,1)\|DECADE(3,1)\|ENHANCING CARBON DIOXIDE(3,1)\|EXPANSION VOLUME(3,1)\|FE2SI2O(3,1)\|FINE POWDER(3,1)\|FLUID CHEMISTRY(3,1)\|GEOLOGICAL SOURCE(3,1)\|GREENHOUSE GAS ENVIRONMENTAL IMPACT(3,1)\|HYDROGEN GAS ABIOTIC PRODUCTION(3,1)\|HYDROGEN GENERATING SERPENTINIZATION REACTION(3,1)\|INCREASED MINERALIZATION(3,1)\|INCREASED REACTIVITY(3,1)\|INORGANIC PRODUCT(3,1)\|INTENDED CARBONATION REACTION(3,1)\|	(US12545576)\|What is claimed is:\|1. A system for sequestering carbon and producing hydrogen and magnetite from rock, the system comprising:\| a source of ore containing olivine or pyroxene;\| a reactor having an inlet that receives ore particles and at least one outlet, the reactor also having at least one additional inlet through which one or more of carbon dioxide or water is introduced, the reactor operable at a first temperature for a first residence time to react carbon dioxide that enters the reactor through the at least one additional inlet with the ore particles to generate magnesium carbonate, the reactor also operable at a second temperature for a second residence time to react water that enters the reactor through the at least one additional inlet with the ore particles to generate magnetite and hydrogen gas; and\| a gas separator that is connected to and in fluid communication with the at least one outlet of the reactor, the gas separator configured to separate hydrogen gas from gases that exit the reactor through the at least one outlet.\|2. The system of claim 1, further comprising a crusher that physically reduces a particle size of the ore introduced therein from the source.\|3. The system of claim 2, further comprising:\| a sieve that receives the ore from the crusher and that allows the ore particles up to a pre-selected size to pass into the reactor,\| wherein the inlet that receives the ore particles is configurable to only receive, from the sieve, the ore particles having a size at or below to the pre-selected size.\|4. The system of claim 3, wherein the pre-selected size comprises a size of between about 25 microns and about 150 microns.\|5. The system of claim 1, wherein a pressure inside the reactor during the second residence time is at or above about 1 bar of carbon dioxide.\|6. The system of claim 5, wherein a pressure inside the reactor during the second residence time is at or above 5 bars of carbon dioxide.\|7. The system of claim 6, wherein a pressure inside the reactor during the second residence time is at or above 10 bars of carbon dioxide.\|8. The system of claim 1, further comprising a magnetic separator that receives material from the at least one outlet of the reactor, the magnetic separator having a magnet that attracts the magnetite and thereby separates the magnetite from the material.\|9. The system of claim 1, further comprising a washer that applies either additional water or an acidic solution to the ore particles prior to their reaction with the carbon dioxide.\|10. The system of claim 1, further comprising a separator that separates at least one of nickel, cobalt, chromium, or rare earth elements from any remaining ore particles removed from the reactor.\|11. The system of claim 1, wherein the reactor includes a first reactor into which the carbon dioxide is introduced and a second reactor into which the water is introduced, the first reactor being operable at the first temperature for the first residence time to react the carbon dioxide that enters the first reactor through the at least one additional inlet with the ore particles, and the second reactor being operable at the second temperature for the second residence time to react the water that enters the second reactor with any remaining ore particles introduced into the second reactor from the first reactor.\|12. The system of claim 1, wherein the water has a pH of between about 8.3 and about 11.1.\|13. The system of claim 1, wherein at least one of the first temperature and the second temperature is no greater than 400° C.\|14. The system of claim 1, wherein at least one of the first temperature and the second temperature is no greater than 300° C.\|15. The system of claim 1, wherein a pressure inside the reactor during the first residence time is at or above about 5 bars of carbon dioxide.\|16. The system of claim 1, wherein the carbon dioxide that is introduced into the reactor is gaseous or supercritical carbon dioxide.\|17. The system of claim 1, further comprising a separator that separates at least one of phosphates, aluminum oxides, precious metals, and other mineral gangue from any remaining ore particles removed from the reactor.\|18. A method for generating hydrogen and magnetite from rock, the method comprising:\| obtaining an ore containing olivine or pyroxene;\| introducing the ore into a reactor that is operable at temperatures above ambient temperature and pressures above atmospheric pressure;\| introducing water into the reactor at a particular temperature for a particular residence time to react with the ore to generate magnetite and hydrogen gas;\| removing, from the reactor, a gas mixture that includes the hydrogen gas;\| separating the hydrogen gas from the gas mixture; and\| removing any remaining ore from the reactor.\|19. The method of claim 18, further comprising washing the ore with either additional water or an acidic solution prior to comminuting the ore into the smaller size fractions.\|20. The method of claim 18, further comprising:\| sieving the ore prior to introducing the ore into the reactor to allow ore particles up to a pre-selected size to pass into the reactor,\| wherein introducing the ore into the reactor comprises introducing, into the reactor, only a subset of the ore having particles up to the pre-selected size.	(US12545576)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This application is a continuation of U.S. application Ser. No. 18/302,702 filed Apr. 18, 2023, which is a continuation of U.S. patent application Ser. No. 17/815,914 filed Jul. 28, 2022, which claims the benefit of U.S. Provisional Patent Application No. 63/203,814 filed Jul. 30, 2021. The entire contents of all of the above applications are incorporated herein by reference.\|(US12545576)\|FIELD OF THE DISCLOSURE\|[0002] One or more embodiments of this disclosure generally relate to systems and methods that produce hydrogen, generate magnetite, and/or derive additional desired products from ores containing olivine or pyroxene (such as mafic and/or ultramafic rocks) through pre-selected chemical processes. In one or more embodiments, the systems and methods facilitate carbonization and/or serpentinization/hydration reactions involving olivine- and pyroxene-rich ores in order to sequester carbon dioxide, liberate hydrogen, generate magnetite and magnesite, and/or derive other desired products, including scarce metals, which are in many cases critical to various green technologies (e.g., batteries, energy storage, photovoltaics) otherwise mined using carbon-intensive methods.\|BACKGROUND\|[0003] The environmental impact of greenhouse gases, primarily carbon dioxide (CO2) and methane (CH4), has been the subject of much public debate over the past several decades. More recently, self-imposed private-sector initiatives and government-mandated regulations to reduce the release of greenhouse gases into the environment have begun to be implemented. In addition to the capture and/or sequestration of carbon dioxide and other greenhouse gases to mitigate their atmospheric release, much research and development effort has been focused on the utilization of alternatives to fossil fuel combustion for energy production in order to reduce the amount of carbon dioxide generated and/or that must be captured and sequestered.\|[0004] Hydrogen (H2) gas holds promise as an energy source (e.g., as hydrogen fuel or through the use of green ammonia) and chemical feedstock (e.g., methanol, ammonia, hydrocarbon fuels) that provides little-to-no greenhouse gas emission upon combustion. Indeed, the combustion of hydrogen gas yields just water as a reaction product. However, hydrogen gas has traditionally been produced using fossil fuels (e.g., via natural gas/methane conversion in a steam reformer), which yields the greenhouse gas carbon dioxide as a reaction product. For example, in the steam-methane reforming reaction mentioned, methane is reacted with steam (i.e., water) to produce hydrogen gas and carbon monoxide. In a subsequent water-gas shift reaction, the carbon monoxide is further reacted with steam to produce carbon dioxide and additional hydrogen gas. The hydrogen gas is subsequently separated from the carbon dioxide through pressure swing adsorption, membrane separation, or another gas separation process. Thus, most hydrogen that is produced in refinery operations, for example, produces greenhouse gases, which must be captured and sequestered to yield meaningful benefit.\|[0005] Alternatively, hydrogen gas may be generated by the electrolysis of water into hydrogen gas and oxygen. The hydrogen gas is subsequently separated from oxygen through pressure swing adsorption, membrane separation, or another gas separation process. Hydrogen production via electrolysis, or partial pyrolysis reactions, requires a substantial amount of electricity. While at least some of the required electricity for hydrogen production via electrolysis and/or partial pyrolysis reactions may be obtained from renewable sources (e.g., wind, solar, and hydroelectric), in practice the majority of the electricity used for this purpose has traditionally been, and continues to be, produced through the combustion of fossils fuels, which also produces greenhouse gases.\|[0006] The abiotic production of hydrogen gas is known to occur in certain geological formations, e.g., at young oceanic crust near a mid-oceanic ridge, as depicted in FIGS. 1A-1D. These natural reactions occur across a range of environmental conditions that include variable pH, oxygen fugacity, chemical composition, and pressure. Such reactions produce variable and complex mineralogy and chemistry but do not predictably produce any specific combination of reaction products. In fact, as generally illustrated in the cross-section photograph of FIG. 2, rock deposits 200 that may yield abiotic hydrogen often contain complex mixtures or layers of difficult-to-extract mineral phases, or will not produce a desired product if other competing reactions are preferred based on in situ geochemical conditions (e.g., variable redox potential (Eh), pH, pore water composition, gas chemical composition, and temperature). For example, hydrogen production is highly variable in nature and its occurrence greatly depends on pH, Eh, and other aspects of fluid geochemistry in pore spaces and at mineral surfaces. Thus, the complex kinetics of reaction phases and the occurrence of competing reactions in natural conditions (e.g., circumneutral pH, variable oxygen fugacity, and variable pore water chemistry) govern the products yielded by these naturally occurring reactions. Certain geological formations and/or the rocks thereof are also known to contain minerals that are conducive to reaction with carbon dioxide under certain conditions to form carbonated mineral phases, e.g., carbonates.\|BRIEF SUMMARY\|[0007] FIG. 3 provides a map that highlights the example locations of selected suitable and/or robust deposits of mafic and ultramafic rock around the world. Olivine- and pyroxene-bearing ores may be found in such mafic and/or ultramafic formations. As can be understood from FIG. 3, sources of mafic and ultramafic igneous rocks may be found in many locations and are quite plentiful, accounting for at least 10% of the continental crust of the Earth, which illustrates the global applicability of solutions described herein. More recently, such sources of mafic and ultramafic igneous rock have garnered interest for their potential exploitation to sequester (mineralize) carbon dioxide in carbonate mineral phases. However, despite significant prior work on carbon sequestration, there is considerable debate about the best mechanistic reactions and optimized rates for carbon mineralization. As such, the economic viability of these processes has not been fully developed, nor has the hydrogen generation and carbon sequestration capacity of mafic and ultramafic rocks been realized. Moreover, no economic use has been identified for the fine-grained carbonated mineral phases that result from carbonization reactions. Rather, proposals have recommended such carbonated mineral phases be used as fill or dumped in oceans or lakes).\|[0008] Despite the theoretical potential for such geological formations and/or the ores thereof to be exploited for geological hydrogen or other products, and for potential carbon sequestration, the processes and kinetics of these reactions has not been rigorously evaluated nor optimized. Further, processes for the production of hydrogen from these geological formations without the occurrence of alternative, and sometimes deleterious, mineral phases (e.g., serpentine, such as antigorite, asbestos) have not been developed. Accordingly, Applicant has recognized a need for systems and methods that exploit certain geological formations and/or the ores thereof to liberate hydrogen, generate magnetite and magnesite, and/or derive other desired products, such as scarce/critical metals from geological formations that include olivine- and pyroxene-rich ores, and in addition, sequester carbon dioxide in magnesite or other mineral phases.\|[0009] The disclosure herein provides one or more embodiments of systems and methods for sequestering carbon, evolving hydrogen gas, and producing magnetite as well as magnesite from olivine- and pyroxene-bearing ores. In addition, precious or scarce metals, such as nickel, cobalt, chromium, and rare earth elements, may be concentrated in the remaining ore, which facilitates their recovery.\|[0010] In an example embodiment, a method is provided for sequestering carbon and producing hydrogen and magnetite. The method includes obtaining an ore that containing olivine or pyroxene. The ore may be comminuted into smaller size fractions, such as by crushing or grinding. The comminuted ore may be introduced into a reactor that is operable at temperatures above ambient temperature and pressures above atmospheric pressure. The method may also include introducing carbon dioxide (or a mixture of carbon dioxide and other gases such as nitrogen (N2), dihydrogen sulfide (H2S), and sulfur dioxide (SO2) into the reactor at a first temperature above ambient temperature for a first residence time to react at least a portion of the carbon dioxide with the ore. The method also includes later introducing water into the reactor at a second temperature for a second residence time to react at least a portion of the water with one or more of the remaining ore to generate at least magnetite and hydrogen gas. Reaction products, including hydrogen gas, magnesium carbonate (magnesite), magnetite, other reaction products, and any remaining ore may be removed from the reactor.\|[0011] In another embodiment, a method is provided for sequestering carbon and generating hydrogen and magnetite from rock. The method includes obtaining an ore that olivine or pyroxene. As above, the ore may be broken down into smaller size fractions, such as by crushing or grinding. The ore is introduced into a first reactor that is operable at a first temperature above ambient temperature and pressures above atmospheric pressure. The method also includes introducing carbon dioxide (or a mixture of carbon dioxide and other gases such as nitrogen (N2), dihydrogen sulfide (H2S), and sulfur dioxide (SO2)) into the first reactor at the first temperature for a first residence time to react at least a portion of the carbon dioxide with the ore to generate at least magnesium carbonate. The remaining ore may be passed to a second reactor. Reaction products from the first reactor may be separated from the remaining ore or may also be passed to the second reactor. The method also includes introducing water into the second reactor at a second temperature for a second residence time to react at least a portion of the water with the remaining ore in the second reactor to produce at least magnetite and hydrogen gas. Reaction products, including hydrogen gas, magnesium carbonate (magnesite), magnetite, other reaction products and any remaining ore may be removed from the second reactor.\|[0012] In yet another embodiment, a system is provided for sequestering carbon and producing hydrogen and magnetite from rock. The system includes a source of ore that contains olivine or pyroxene. The system may include a crusher or grinder used to physically reduce the particle size of the ore introduced therein from the source. The system may include a sieve used to receive the ore from the crusher and configured to allow ore particles up to a pre-selected size to pass therethrough. The system also includes a reactor having an inlet that receives ore particles up to the pre-selected size from the sieve and at least one outlet. The reactor also has at least one additional inlet through which one or more of carbon dioxide or water may be introduced (and in some embodiments, the reactor may comprise two reactors: a first reactor having an additional inlet through which carbon dioxide may be introduced, and a second reactor having another additional inlet through which water may be introduced). The reactor is operable at a first temperature for a first residence time to react at least a portion of any received carbon dioxide with the ore in the first reactor to generate at least magnesium carbonate. The reactor is also operable at a second temperature for a second residence time to react at least a portion of any water that enters the reactor through the at least one additional inlet with any ore within the reactor to generate magnetite and hydrogen gas. In one or more embodiments, the system also includes a gas separator that is connected to and in fluid communication with the at least one outlet of the reactor. The gas separator is configured to separate hydrogen gas from gases that exit the reactor through at least one outlet of the reactor.\|[0013] Corresponding means for performing these various steps are set forth below.\|[0014] The foregoing brief summary is provided merely for purposes of summarizing some example embodiments described herein. Because the above-described embodiments are merely examples, they should not be construed to narrow the scope of this disclosure in any way. It will be appreciated that the scope of the present disclosure encompasses many potential embodiments in addition to those summarized above, some of which will be described in further detail below.\|(US12545576)\|BRIEF DESCRIPTION OF THE FIGURES\|[0015] Having described certain example embodiments in general terms above, reference will now be made to the accompanying drawings, which are not necessarily drawn to scale. Some embodiments may include fewer or more components than those shown in the figures.\|[0016] FIGS. 1A, 1B, 1C, and 1D illustrate cross-sectional representations of young oceanic crust and associated structures positioned near a theoretical mid-oceanic ridge that may produce and/or host abiotic hydrogen production.\|[0017] FIG. 2 illustrates an example cross-section of serpentinized ultramafic rock.\|[0018] FIG. 3 illustrates a map with locations of suitable olivine- and pyroxene-bearing localities throughout the world.\|[0019] FIG. 4A provides an example flow diagram illustrating a sequence of operations performed by a system to enhance carbon dioxide sequestration, hydrogen gas evolution, and magnetite and magnesite production using a single reactor, in accordance with some example embodiments described herein.\|[0020] FIG. 4B provides an example flow diagram illustrating a sequence of operations performed by a system to enhance carbon dioxide sequestration, hydrogen gas evolution, and magnetite/magnesite production using multiple reactors, in accordance with some example embodiments described herein.\|[0021] FIG. 5 illustrates an example flowchart for enhancing carbon dioxide sequestration, hydrogen gas evolution, and magnetite/magnesite production, in accordance with some example embodiments described herein.\|[0022] FIG. 6 illustrates an example flowchart for acquisition and preparation of source rock for reaction, in accordance with some example embodiments described herein.\|[0023] FIG. 7 illustrates an example flowchart for processing rock remaining following any carbon dioxide and/or water reactions, in accordance with some example embodiments described herein.\|(US12545576)\|DETAILED DESCRIPTION\|[0024] Some example embodiments will now be described more fully hereinafter with reference to the accompanying figures, in which some, but not necessarily all, embodiments are shown. Because inventions described herein may be embodied in many different forms, the invention should not be limited solely to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will satisfy applicable legal requirements.\|Overview\|[0025] Applicant recognized that despite the significant theoretical potential of mafic and/or ultramafic igneous rocks (or, more broadly, olivine- and pyroxene-bearing ores, such as those with elevated iron content), as described above, to serve as geological sources for economic geological hydrogen, to be exploited as natural sources and catalysts for hydrogen and magnetite production, and to be exploited for carbon sequestration, the optimal processes and kinetics for these reactions have not been rigorously evaluated nor optimized. Specifically, process steps to enhance both carbon sequestration and the production of hydrogen, magnetite, magnesite, and/or other minerals from these types of rocks—without the formation of alternative (and sometimes deleterious, e.g., serpentine, asbestos) mineral phases—have not been developed.\|[0026] Further, Applicant is unaware of any prior attempts to use an optimized chemical process of carbon mineralization to enhance the kinetics of hydrogen and magnetite production, or to regulate the chemical species of the resulting reaction products (e.g., prevent the formation of serpentine and asbestos).\|[0027] In various embodiments disclosed herein, carbon dioxide may be sequestered, and hydrogen, magnetite, and other scarce metals may be produced economically (and with a neutral to net-negative carbon footprint) using olivine- and pyroxene-rich ores through sequential carbonation and serpentinization reactions in a controlled environment. Thus, Applicant has developed an engineering process that employs sequential reactions to exploit the potential for olivine- and pyroxene-rich ores to both sequester carbon dioxide dominantly as magnesite or other carbonate minerals, as well as liberate hydrogen, magnetite, and/or other desirable minerals/scarce metals. Applicant further recognized that additional process steps applied to the olivine- and pyroxene-rich ores may enhance the concentration and recovery of precious or scarce metals (e.g., nickel, cobalt, chromium, lithium, and rare earth elements.), which are needed for renewable energy and energy storage, among other uses.\|[0028] Applicant discovered that the serpentinization reaction process can be advantaged such that the chemical activity and commensurate rates of reactions between water and fayalite and/or ferrosilite may be enhanced by first removing a significant component of forsterite from the olivine mineral phase and increasing the comminution of mineral grains by inducing the described chemical reactions. In this way, the fayalite and/or ferrosilite in the igneous rock is concentrated and/or becomes less obscured by adjacent minerals, e.g., forsterite. This process benefits the reaction in two ways: first, by enhancing the surface area of fayalite and/or ferrosilite exposed for the reaction; and second, by pre-concentrating the reactant (iron-rich olivine (fayalite) or pyroxene (ferrosilite)) of choice. Thus, in one or more embodiments, forsterite and/or enstatite are at least partially removed prior to reacting the fayalite and/or ferrosilite with water.\|[0029] Some primary differentiators that demonstrate the value of example ex situ engineered embodiments that produce hydrogen, magnesite, magnetite, and critical metals via this pathway include: 1) the immense geological scalability of such embodiments once the “serpentinization” processes are optimized to produce the desired products (hydrogen, magnetite, scarce metals), as opposed to alternative mineral phases such as serpentine, asbestos, etc.; 2) the potential to permanently and verifiably sequester CO2 in a mineralized form and hence produce hydrogen, magnetite, and scarce metals in a carbon-negative process; and 3) the price point of potentially scalable “green” or “golden” hydrogen (i.e., carbon negative hydrogen), magnetite, and scarce metals, which can be greatly offset by considering other values streams generated using the quarrying concept (i.e., the sale of aggregate or higher value utilization of magnesite).\|[0030] Although a high-level explanation of the operations of example embodiments has been provided above, specific details regarding the configuration of such example embodiments are provided below.\|Serpentinization and Carbonation Reactions\|[0031] The disclosure herein provides one or more embodiments of systems and methods that facilitate the production of hydrogen, magnetite, and/or other desired minerals through serpentinization reactions involving olivine- and pyroxene-rich ores generally found in mafic and/or ultramafic igneous rock, or of any other rock assemblages containing such olivine- and pyroxene-rich ores. Table 1, provided below, gives representative serpentinization reactions involving fayalite (Fe2SiO4) and/or ferrosilite (Fe2Si2O6). Fayalite is a mineral phase that is the iron-rich endmember of the olivine solid solution series and is abundant in olivine-rich orc. Ferrosilite is the iron-rich endmember of the orthopyroxene solid solution series and is associated with pyroxene-rich ore. Fayalite and ferrosilite are commonly found together in mafic and ultramafic igneous rocks. Under certain conditions, water reacts with fayalite and ferrosilite to generate magnetite (Fe3O4), silica (SiO2), and hydrogen gas (H2) in the appropriate stoichiometric ratios. In each case, two moles of hydrogen gas are produced from three moles of either fayalite or ferrosilite mineral.\|[0032] TABLE 1 Hydrogen-Generating Serpentinization ReactionsSerpentinization Reactions Moles of MineralSerpentinizationIgneousMolesMineralPhaseReactionMineralof H2 OlivineFayalite3 Fe2 + 2 H2O →32 2 Fe3O4 + 3 SiO2 + 2 H2 PyroxeneFerrosilite3 Fe2Si2O6 + 2 H2O →32 2 Fe3O4 + 6 SiO2 + 2 H2 \|[0033] In one or more embodiments, the disclosed systems and methods may also facilitate the sequestration of gaseous carbon dioxide as mineralized carbonates through carbonation reactions involving the magnesium-rich endmember of olivine- and pyroxene-rich ores found typically in mafic and/or ultramafic rock. Table 2, provided below, gives representative carbonation reactions involving forsterite (Mg2SiO4) and enstatite (Mg2Si2O6), as well as illustrating the potential for carbonation during reaction with antigorite (Mg3Si2O5(OH)4) that can be formed as an accessory mineral phase in natural systems in which fluid conditions are not idealized for the formation of magnesite. Forsterite is a mineral phase that is the magnesium-rich endmember of the olivine solid solution series associated with olivine-rich ore. Enstatite is a mineral phase that is the magnesium-rich endmember of the orthopyroxene solid solution series associated with pyroxene-rich ore. Antigorite is an example mineral phase that is associated with serpentine. Under certain conditions, carbon dioxide reacts with forsterite and enstatite, and/or other accessory mineral phases (e.g., antigorite) to generate at least magnesium carbonate (MgCO3) and silica (SiO2) in appropriate stoichiometric ratios. The reaction of antigorite with carbon dioxide further yields a stoichiometric quantity of water and is shown to illustrate serpentinization reactions that occur in natural systems in which pH, Eh, temperature, pressure, and fluid chemistry cannot be optimized. In the case of the idealized carbonization reaction involving forsterite and enstatite, two moles of carbon dioxide gas are converted to magnesium carbonate (magnesite) per mole of either forsterite or enstatite mineral.\|[0034] TABLE 2 Carbon-Sequestering Carbonation ReactionsDecarbonation Reactions Moles of MineralDecarbonationIgneousMolesMineralPhaseReactionMineralof CO2 OlivineForsteriteMg2SiO4 + 2 CO2 →12 2 MgCO3 + SiO2 PyroxeneEnstatiteMg2Si2O6 + 2 CO2 →12 2 MgCO3 + 2 SiO2 SerpentineAntigoriteMg3Si2O5(OH)4 +13 3 CO2 → 3 MgCO3 + 2 SiO2 + 2 H2O \|[0035] In nature, and as previously described, the above-described serpentinization and carbonization reactions occur, but only as a subset of a variety of reactions occurring across a range of environmental conditions in the subsurface or at surface conditions of the earth. As a result, the environmental conditions are often variable and reactions kinetics and pathways are far from ideal. Accordingly, natural reactions are based on the variable (and often dynamic, i.e., changing with time) pH, oxygen fugacity, temperature, pore water chemical composition, gas chemical composition, and pressure found in nature, specifically in the subsurface. The multitude of reactions and potential pathways for those reactions occurring in nature lead to the formation of variable and complex chemistry and assemblages of minerals, but do not predictably produce any specific combination of usable reaction products. Instead, natural systems, which evolve through time and under varying reaction conditions produce complex (and often heterogeneous) complexes of varying mineral assemblages and products of reactions that did not follow the idealized reactions described above, or are slower to reach thermodynamic equilibrium.\|[0036] With respect to olivine and pyroxene mineralogy and chemistry, olivine is a solid solution series (X2SiO4, where X═Mg2+ or Fe2+) between a magnesium silicate (forsterite) and an iron silicate (fayalite) and pyroxene (i.e., orthopyroxene) is a solid solution series (X2Si2O6, where X═Mg2+ or Fe2+) between a magnesium silicate (enstatite) and an iron silicate (ferrosilite). In the olivine-rich deposits of interest, fayalite and ferrosilite are usually the minor constituent and typically range in concentration from 6% to 20%, with the lower range concentrations appearing more commonly in nature. Consequently, the thermochemical activities of fayalite and ferrosilite are relatively low compared to those of the forsterite or enstatite, respectively. Thus, if the olivine or pyroxene obtained from a quarry is crushed and reacted with water at favorable reaction conditions (i.e., controlled for temperatures, pressures, Eh, pH, and fluid composition, then a serpentinization reaction will proceed at a relatively low rate due to relatively low thermochemical activity and commensurately low rates of reactions with fayalite or ferrosilite. Nevertheless, when completed, the reaction produces magnetite, silica, and hydrogen (from the reaction of fayalite or ferrosilite with water) may be separated (magnetically or gravimetrically) from forsterite, enstatite, or magnesite. The mixture of olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite) minerals, however, constitutes an almost an “ideal” mixture that is exceedingly rare in natural systems. However, in an ideal mixture, the chemical activity varies linearly with the mole fraction and is roughly equal to the mole fraction. Thus, the chemical activity and reaction rate can be enhanced by pre-concentrating the abundance of olivine and pyroxene from the bulk ore and specifically the abundance of the iron-rich endmembers of both the olivine and pyroxene solid solution series.\|Ex Situ Sequestration of Carbon Dioxide and Generation of Hydrogen\|[0037] In various embodiments contemplated herein, carbon dioxide may be mineralized, and hydrogen, magnesite, magnetite, and critical metals may be produced economically (and with an overall neutral to net-negative carbon footprint) by an engineered system that causes sequential reactions in the manner shown in the flow diagrams illustrated in FIGS. 4A, 4B, and described in connection with the flowcharts provided in FIGS. 5, 6, and 7.\|[0038] FIG. 4A illustrates a flow diagram of one embodiment 400′ of a system for enhancing the production of hydrogen gas and magnetite from rock that contains a mixture of olivine (e.g., fayalite and forsterite) and pyroxene (e.g., ferrosilite and enstatite) minerals. A source of olivine- and/or pyroxene-rich ores 402 may be fed or introduced into a crusher or grinder 406 that reduces the size of the received ore into smaller size fractions. In one or more embodiments, a washer 404 may optionally be used to wash the ore with water or a mildly acidic solution to remove any contaminants therefrom and prepare the ore for carbonation reactions. The crushed or ground rock is then introduced into a sieve 408 or other such separator that segregates the rock into pre-selected particle ranges. In one or more embodiments, the sieves or grates thereof are sized to pass 150-, 80-, and even 45-micron grains, although different sizing can be utilized. In at least one embodiment, the comminuted rock is a powder or has a powder-like particle size range. Rock that does not pass through the sieve may be returned to the crusher or grinder 406 via a recycle loop 410 to be reduced further in size. The subset of the rock having particles within a pre-selected particle range of the sieve 408, e.g., 150-micron, 80-micron, 45-micron, or any size therebetween, is then fed or introduced into a reactor 412.\|[0039] The reactor 412 may be a rotary kiln, a toroidal fluidized bed, a fluidized bed, or another reactor known to those skilled in the art. The reactor 412 may have an inlet that receives ore (or ore particles) at least one outlet, from which any remaining ore may be removed following reaction within the reactor 412. The reactor 412 may further have at least one additional inlet through which one or more of carbon dioxide or water can be introduced into the reactor 412. The reactor 412 may be operable at a first temperature for a first residence time to react carbon dioxide that enters the reactor 412 through the at least one additional inlet with ore disposed within the reactor 412 to generate magnesium carbonate. The reactor 412 may further be operable at a second temperature for a second residence time to react water that enters the reactor through the at least one additional inlet (which may be the same inlet by which carbon dioxide enters the reactor 412 or a different inlet) with ore disposed within the reactor 412 to generate magnetite and hydrogen gas.\|[0040] In a first reaction step, carbon dioxide is introduced into reactor 412 with the crushed/ground rock. Water (approximately 10 liters of water per kilogram) may be applied (sprayed or washed) to the crushed/ground rock by washer 404 either before or after placement of the rock into the reactor 412. The wetting of the powdered rock with water allows for the dissolution of gaseous CO2 to carbonic acid (H2CO3) on the wet surfaces of the mineral grains, which enhances the reactivity of the carbon dioxide with the forsterite mineral found therein. In at least one embodiment, the pH of the water applied to the comminuted rock may be between about 4.8 to about 6.5. Water in this pre-selected pH range further enhances the reaction between the carbon dioxide and the forsterite mineral. During this first reaction step, the reactor is operated at a pre-selected temperature (>90° C.) and pressure (greater than approximately five bars) to facilitate the carbonation reaction with respect to the forsterite mineral found in the rock. In one or more embodiments, the reactor 412 is operated at a temperature of between about 100° C. to about 400° C. and at a pressure of between about five and up to at least 100 bars (e.g., about 40, 50, 75 or even 100 bars); note the upper limit of pressure can be extended to considerably higher pressures if the reactor 412 and associated components are able to withstand such pressures. Increasing pressure in this fashion will produce a corresponding enhancement of the carbonation reaction being prompted at this stage of the process. In other embodiments, the operating pressure of the reactor 412 may be as low as 35 bars, as low as 30 bars, as low as 25 bars, as low as 20 bars, as low as 15 bars, as low as 10 bars, as low as 5 bars, or even lower (˜1 bar), and may still prompt the intended carbonation reactions, albeit at commensurately lower rates of reaction. As provided in Table 2 above, the reaction of carbon dioxide with the forsterite (Mg2SiO4) produces magnesium carbonate (MgCO3) and silicon dioxide (SiO2) as reaction products. In this way, the forsterite mineral of the mafic and/or ultramafic rock is used to permanently sequester CO2 in the form of an insoluble magnesium carbonate mineral lattice, which is a solid that that can be useful as a raw material, placed in a landfill, ocean, lake, or otherwise easily stored. By reacting the crushed/ground rock containing the forsterite with carbon dioxide at favorable conditions of temperature, pressure, Eh, and pH, the forsterite can be altered to magnesite following reaction with carbon dioxide.\|[0041] It will be understood that, although this first reaction step favorably enhances the comminution of source rock and better prepares any remaining rock for the second reaction step described below, some embodiments may not perform this first reaction step, and instead may simply comminute the source rock, which itself prepares the source rock for the second reaction step, as illustrated by way of example in the Example Implementation section below. Of course, in other embodiments, the source rock may not need to undergo an initial comminution step, but may instead simply be initially processed using the first reaction step described herein, which itself fosters comminution of the source rock and thus prepares it for more effective reaction in the second reaction step described below. Both comminution of the source rock and the carbonation reactions occurring during the first reaction step favorably dispose any remaining rock for the section reaction step below; accordingly, various combination of comminution and the first reaction step may be employed in various scenarios based on the desired results of a given implementation.\|[0042] In a second reaction step, water is thereafter introduced into reactor 412 with the crushed/ground rock, which may in some embodiments still contain the magnesium carbonate and silicon dioxide from the first reaction step, the fayalite and/or ferrosilite minerals in the original crushed/ground rock, and any other minerals/ores found in the original crushed/ground rock. In some embodiments, magnesium carbonate and silicon dioxide from the first reaction step can be separated from the residual iron silicate phases based on their respective densities. In one or more embodiments of these processes, the water that is added to the reactor 412 may have a low oxygen fugacity (e.g., it may be obtained from municipal wastewater treatment, groundwater, geothermal water, mine waters, another industrial water source, or by reacting a municipal water (i.e., “tap water”) over a bed of copper at temperatures exceeding 125° C., or by another mechanism) and a pH of between about 8.3 and about 11.1 (with the specified pH being artificially attained, such as by adding sodium bicarbonate to the water, or naturally obtained, such as where the water with such pH range may be found in certain sources of water and wastewater). During this second reaction step, the reactor is operated at a pre-selected temperature and pressure (˜1 to 20 bars) to facilitate the serpentinization of the fayalite and/or ferrosilite minerals in the rock. In one or more embodiments, the reactor 412 is operated at a temperature in the range of between about 80° C. and about 400° C. As provided in Table 1 above, the reaction of water with the fayalite (Fe2SiO4) and/or ferrosilite (Fe2Si2O6) produces hydrogen gas, variable mixtures of nitrogen (N2), carbon dioxide (CO2), silicon dioxide, and magnetite (Fe3O4) as reaction products. The molecular and isotopic composition of hydrogen formed during this ex situ process will be determined by the temperature conditions of the reaction (e.g., ˜175° C.) and the composition of the initial water, wherein the fractionation factors (a) between H2O and H2 follow the fractionation factors observed for standard geothermometers. The hydrogen gas, along with any other gases in the reactor 412, such as unreacted carbon dioxide (CO2), sulfur dioxide (SO2), or dihydrogen sulfide (H2S) or inert gases (e.g., nitrogen (N2), argon (Ar) from the first reaction step, are passed to a gas separator 414. The gas separator 414 may be a membrane unit, a pressure swing adsorption, or a cryogenic separation unit that can separate the hydrogen gas from other gases, e.g., atmospheric gases, that may also be present in the reactor 412. The gas separator 414 may be connected to and in fluid communication with at least one outlet of the reactor 412 and configured to separate hydrogen gas from gases that exit the reactor 412 through the at least one outlet.\|[0043] In at least one embodiment, gases that may be present in the reactor 412 prior to the second reaction may be evacuated prior to the second reaction, such as by pulling a vacuum on the reactor 412. Without these contaminant gases in the reactor 412 (e.g., N2 or CO2), the hydrogen gas that is formed as a result of the serpentinization reaction with water may be the only gas present after the second reaction step. In such case, the gas separator 414 may not be needed to segregate the hydrogen gas as a product. After the second reaction step, the magnesium carbonate, silicon dioxide, magnetite, and any remaining rock/unreacted ore may be removed from the reactor 412. In some embodiments, magnesium carbonate (i.e., magnesite) and silicon dioxide (i.e., quartz) may be separated from iron silicates and other mineral phases before the material is placed in reactor 412. The magnetite, which represents a valuable product/feedstock for the iron industry (with particular value in direct reduced iron manufacturing), may be recovered from the magnesium carbonate, silicon dioxide and any remaining rock/ore by, for example, magnetic separation or other density separation techniques. A magnetic separator 416 may be used to selectively attract the magnetite through the use of one or more magnets and thereby physically remove the magnetite from the other non-metallic ore. In one or more embodiments, the solid products, e.g., the magnetite, magnesium carbonate, silicon dioxide, and any remaining, unreacted ore/rock may be further crushed or ground (not shown in FIG. 4A) to facilitate the removal of magnetite particles from the other solids in the magnetic separator 416 or conduct secondary recovery of other minerals or metal-rich phases. The separated hydrogen gas from gas separator 414 and the magnetite recovered via the magnetic separator 416 are valuable products whose production and recovery from mafic and/or ultramafic rock are enhanced by the disclosed sequential carbonization and serpentinization reactions disclosed herein.\|[0044] The remaining magnesium carbonate (in which the carbon is permanently sequestered in the mineral phase), silicon dioxide, and any unreacted rock/ore may be used as an aggregate material and/or placed in landfill or otherwise disposed of. In one or more embodiments, the magnesium carbonate and silicon dioxide may be separated (based on density separation techniques such as heavy liquids or other gravity separation, or sluicing) and removed from the remaining rock/gangue (gangue: collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) materials. As further discussed below, magnesium carbonate (or magnesite) is useful in the manufacturing of pharmaceuticals, agricultural lime, and fertilizers (to neutralize acidification caused by fertilizer use), ceramics and ceramic brick, and as flux used in iron and steel manufacturing. Magnesite may also be used as a partial lime substitute to enable lower carbon emissions that result from the lower temperatures required to make magnesium oxide (MgO) as compared to calcium oxide (CaO) for cement manufacturing. Further, magnesite can be used as a carbon negative concrete filler and cement or aggregate substitute in concrete.\|[0045] In one or more embodiments, rather than landfilling or otherwise using the bulk of the magnesium carbonate, silicon dioxide, and any unreacted rock/ore, the rock and/or gangue material from the first reaction phase is further processed to separate and remove specific valuable components therefrom. For example, elevated concentrations of certain precious metals (e.g., nickel, cobalt, chromium, and rare earth elements) in mafic and ultramafic rocks are further concentrated in this “slag” material. In at least one embodiment, highly elevated metal enrichments, that include but are not limited to phosphates, aluminum oxides, precious metals, and other mineral gangue may be separated from the remaining rock/ore by, for instance, heavy liquid separation or other gravity separation, or sluicing in a separator 418. Through gravity separation, the various metals and other valuable components are ground into fine particles and separated based on their individual specific weights.\|[0046] As illustrated in FIG. 4A, the first and second reactions can both occur in the same reactor 412, which may be a rotary kiln, fluidized bed, toroidal bed, or other reactor as described previously, in which case the reactions may be run sequentially, and all products separated at the completion of both reactions. In one or more embodiments (not shown in FIG. 4A), the reaction products (i.e., magnesium carbonate and silicon dioxide) may be separated after the first reaction step and prior to the second reaction step using established density separation techniques such as heavy liquid separation or other gravity separation, or sluicing. In other embodiments, as shown in FIG. 4A, the reaction products remain in the reactor during the second reaction step. Even if the reaction products are not physically separated, the thermochemical activity and reaction rates of fayalite and/or ferrosilite will increase according to the newly exposed surface area of fayalite and/or ferrosilite minerals. In other words, the reactivity of the serpentinization reactions with respect to the fayalite and/or ferrosilite minerals will proceed according to the now higher molar fraction of fayalite and/or ferrosilite in the solid solution (i.e., the number and/or extent of alternative side reactions has been reduced). With respect to the upper limit of the fully separated (e.g., using established density separation techniques such as heavy liquid separation or other gravity separation, or sluicing) or exposed fayalite and/or ferrosilite, the thermochemical activity of the powdered material should approach unity of the pure phase mineral, or mixtures of fayalite and/or ferrosilite mineral phases. Thus, the first reaction step involving the reaction of the forsterite with carbon dioxide increases the thermochemical driver for the second reaction step, which is the serpentinization/hydration reaction of the fayalite and/or ferrosilite with water, by reducing the availability of forsterite and increasing the exposed surface area of fayalite and/or ferrosilite minerals. The former increases the kinetic rate by driving the thermochemical activity toward that of a pure compound, while the latter enhances chemical activity by increasing the surface area available for reaction.\|[0047] FIG. 4B illustrates a flow diagram of another embodiment 400″ of a system of enhancing the production of hydrogen gas and magnetite from a source rock that contains a mixture including olivine (fayalite and forsterite) and/or pyroxene (ferrosilite and enstatite) minerals. The flow diagram of FIG. 4B is similar to that of FIG. 4A, except that the first reaction step occurs in a first reactor 412′ and the second reaction step occurs in a second reactor 412″. The first reactor 412′ facilities the carbonation reaction between the forsterite mineral and carbon dioxide. The crushed/ground ore of a uniform or pre-selected particle size range is passed from the sieve 408 or other particle size separator into the first reactor 412′. Carbon dioxide is pumped into the first reactor 412′ in above stoichiometric ratios to facilitate the carbonization reactions listed in Table 2. After the first reaction has occurred, the magnesium carbonate and silicon dioxide products, along with the unreacted fayalite and/or ferrosilite, and other remaining ore, are passed to the second reactor 412″.\|[0048] Continuing with FIG. 4B, the second reactor 412″ facilitates the serpentinization reaction between the fayalite and/or ferrosilite mineral phases and water (or steam). The reaction products and remaining rock/ore from the first reactor 412′ are introduced into the second reactor 412″. Water is pumped into the second reactor 412″ in above stoichiometric ratios (>˜20 liters/kg of rock) to facilitate the serpentinization reactions listed in Table 1. After the second reaction has occurred, the reactor gases, including the hydrogen gas evolved during the second reaction step, are passed or routed to a gas separator 414, as described above with respect to FIG. 4A. Likewise, the solid reaction products, including magnesium carbonate, silicon dioxide, magnetite, as well as any unreacted ore/rock are passed to a magnetic separator 416, as described above with respect to FIG. 4B. Other than the use of two reactors 412′ and 412″ in place of one reactor 412, as described above, the embodiments represented by FIGS. 4A and 4B are similar. It should be noted that the configuration of the system of FIG. 4B provides a semi-continuous method in that the separate process vessels, e.g., reactors 412′ and 412″, are dedicated to differing portions of the method.\|[0049] FIGS. 5, 6, and 7 illustrate flowcharts of various embodiments for enhancing the production of hydrogen gas, magnetite, magnesite, and scarce metal resources from mafic and ultramafic igneous rock that contains a mixture of olivine (fayalite and forsterite) and pyroxene (ferrosilite and enstatite) minerals. As previously disclosed in connection with FIG. 3, olivine- and/or pyroxene-rich ores may be found in numerous locations around the world. At block 502, such olivine- and/or pyroxene-rich ore may be acquired from geological sites containing high concentrations of such rocks in one or more of these areas. FIG. 6 illustrates this rock acquisition operation in greater detail. As shown at block 602, the olivine- and/or pyroxene-rich source rock may be acquired in any manner known to those skilled in the art, such as by underground mining, strip mining, quarrying, outcrop quarrying, or the use of waste (i.e., mine tailings), etc. The source rock may be transported, e.g., by barge, train, truck, etc., to a facility to further process the rock. In one or more embodiments, the source rock may be processed in proximity to the location where the rock is acquired. The source rock may be processed by crushing and/or grinding the rock at block 606 into smaller size fractions. In addition to creating uniform or near uniform sizing, such comminution also helps to expose the minerals, such as olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite), that are contained within the rock. If the rock is processed in proximity to the geological site from which the rock originated, then the processed rock may then be transported to a facility having a system to further extract hydrogen, magnetite, and other valuable products from the ore according to a method disclosed herein (not shown in FIGS. 5 and 6). At block 608, the crushed and/or ground source rock may be further processed by sieving or otherwise segregating the rock according to size. In one or more embodiments, the crushed and/or ground rock may be washed with water or a slightly acidic solution to clean the surfaces thereof of dust, dirt, or other contaminants. As illustrated at block 604, such washing may be conducted before the rock is crushed and/or ground and can also benefit from agitation.\|[0050] The crushed and/or ground rock is then introduced into a reactor at block 610 in which the rock is reacted with carbon dioxide and water to produce magnesium carbonate and hydrogen gas, among other products, in stoichiometric proportions via the carbonation reactions described in Table 2. The crushed/ground rock may be transported between and introduced into the reactor at block 610 by conveyor, by machinery placement, etc. A slightly acidic water solution, as previously described may be applied, e.g., by washing, spraying, or soaking, onto the outer surfaces of the rock. Such application may be before or after the rock is deposited in the reactor. The air in the reactor, including oxygen therein, may be evacuated from the sealed reactor with the rock disposed therein (e.g., by applying a vacuum to the reactor) or purged using reaction gas (e.g., N2) prior to commencing the reaction. Returning to FIG. 5, block 504 describes that carbon dioxide (CO2) is introduced into the reactor to begin the first reaction phase. The carbon dioxide may be gaseous or supercritical as previously described. A greater-than-stoichiometric portion of carbon dioxide is added as compared to the amount of rock (and specifically forsterite concentration therein) in the reactor in order to ensure that the carbon dioxide does not limit the carbonation reaction and to benefit from increased reactivity that is observed to occur at elevated pressures of CO2 and/or super-critical CO2. At block 504, the reactor is operated at one or more pre-selected temperatures and pressures, as described above, for a first residence time in order to sufficiently react the carbon dioxide with the forsterite mineral to produce magnesium carbonate and silicon dioxide reaction products. At the end of the first residence time, the gas phase from the reactor may be evacuated by, e.g., applying a vacuum or gas purging operation, to remove the excess unreacted carbon dioxide and any other gases evolved via the carbonation reactions of the first reaction phase.\|[0051] Continuing with FIG. 5, at block 506, water is introduced to the reactor after the first residence time. In one or more embodiments, the water is a low oxygen fugacity water that is prepared or obtained as described in greater detail above. Again, a greater-than-stoichiometric portion of water (>˜20 liters/kg of rock) is added as compared to the amount of rock (and specifically fayalite and/or ferrosilite concentrations therein) in the reactor in order to ensure that the water does not limit the serpentinization reaction. At block 506, the reactor is operated at one or more pre-selected temperatures and pressures, as described above, for a second residence time in order to sufficiently react the water with the fayalite and/or ferrosilite minerals (now having additional exposed surface area and more optimized chemical activity due to the first reaction phase) to produce at least hydrogen gas and magnetite reaction products.\|[0052] At block 508, the gas phase is removed from the reactor either during or at the completion of the second reaction phase. This gas phase, which is rich in hydrogen gas (and may contain small quantities of trace gases, e.g., N2, Ar, CO2) may be further purified through gas separator 414 (as shown in FIG. 4A and FIG. 4B). The gas separator 414 may be a pressure swing adsorption unit, a membrane separation unit, a cryogenic separation unit, or any other gas separation unit known to those skilled in the art. If the gas phase was not evacuated from the reactor between the first reaction phase and the second reaction phase, then some carbon dioxide and/or other gases, e.g., reaction gases, may contaminate the hydrogen gas evolved in the reactor via the serpentinization reactions of the second reaction phase.\|[0053] At block 510, the remaining rock within the reactor may be further processed to remove the magnesium carbonate/magnesite, the iron oxide/magnetite, the silicon dioxide, any remaining ore and/or slag material from the reactor. These operations are described in detail in connection with FIG. 7. Block 702 illustrates that the remaining rock in the reactor may be removed for further processing. Such removal may include removal by mechanical machinery, which picks up, rakes, or gravity feeds the material from the reactor into a container or onto a conveyor. In particular, at block 702 the solid reaction products (i.e., magnesite, magnetite, etc.), the remaining ore, and any slag material may be passed to a magnetic separator 416 (as shown in FIG. 4A and FIG. 4B) in order to separate the magnetite from the other materials via attraction of the magnetically susceptible iron oxide to a magnetic field (see block 704). The solid material removed from the reactor at block 702 may undergo additional crushing and/or grinding in order to create a fine powder to facilitate removal of valuable components thereof (not shown in FIGS. 5 and 7). At block 706, any precious or scarce metals that are now more concentrated in the remaining ore and/or gangue (collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) material after magnetite removal may be separated and removed based on density separation techniques such as heavy liquid separation or other gravity separation, or sluicing; an example of gravity separation using a gravity separator is shown in 480. Finally, as shown in block 708, the remaining rock, containing remaining magnesium carbonate (in which the carbon is permanently sequestered in the mineral phase), silicon dioxide, and any unreacted rock/ore may be used as an aggregate material and/or placed in landfill or otherwise disposed of. As noted previously, in some embodiments the magnesium carbonate and silicon dioxide may be separated (based on density separation techniques such as heavy liquids separation, or other gravity separation, or sluicing) and removed from the remaining rock/gangue (gangue: collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) materials for separate dispositioning.\|[0054] FIGS. 5, 6, and 7 illustrates operations performed in various example embodiments. It will be understood that each flowchart block, and each combination of flowchart blocks, may be implemented by various means. The flowchart blocks support combinations of means for performing the specified functions and combinations of operations for performing the specified functions. In some embodiments, some of the operations above may be modified or further amplified. Furthermore, in some embodiments, additional optional operations may be included. Modifications, amplifications, or additions to the operations above may be performed in any order and in any combination.	(US12545576)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This application is a continuation of U.S. application Ser. No. 18/302,702 filed Apr. 18, 2023, which is a continuation of U.S. patent application Ser. No. 17/815,914 filed Jul. 28, 2022, which claims the benefit of U.S. Provisional Patent Application No. 63/203,814 filed Jul. 30, 2021. The entire contents of all of the above applications are incorporated herein by reference.\|(US12545576)\|FIELD OF THE DISCLOSURE\|[0002] One or more embodiments of this disclosure generally relate to systems and methods that produce hydrogen, generate magnetite, and/or derive additional desired products from ores containing olivine or pyroxene (such as mafic and/or ultramafic rocks) through pre-selected chemical processes. In one or more embodiments, the systems and methods facilitate carbonization and/or serpentinization/hydration reactions involving olivine- and pyroxene-rich ores in order to sequester carbon dioxide, liberate hydrogen, generate magnetite and magnesite, and/or derive other desired products, including scarce metals, which are in many cases critical to various green technologies (e.g., batteries, energy storage, photovoltaics) otherwise mined using carbon-intensive methods.\|BACKGROUND\|[0003] The environmental impact of greenhouse gases, primarily carbon dioxide (CO2) and methane (CH4), has been the subject of much public debate over the past several decades. More recently, self-imposed private-sector initiatives and government-mandated regulations to reduce the release of greenhouse gases into the environment have begun to be implemented. In addition to the capture and/or sequestration of carbon dioxide and other greenhouse gases to mitigate their atmospheric release, much research and development effort has been focused on the utilization of alternatives to fossil fuel combustion for energy production in order to reduce the amount of carbon dioxide generated and/or that must be captured and sequestered.\|[0004] Hydrogen (H2) gas holds promise as an energy source (e.g., as hydrogen fuel or through the use of green ammonia) and chemical feedstock (e.g., methanol, ammonia, hydrocarbon fuels) that provides little-to-no greenhouse gas emission upon combustion. Indeed, the combustion of hydrogen gas yields just water as a reaction product. However, hydrogen gas has traditionally been produced using fossil fuels (e.g., via natural gas/methane conversion in a steam reformer), which yields the greenhouse gas carbon dioxide as a reaction product. For example, in the steam-methane reforming reaction mentioned, methane is reacted with steam (i.e., water) to produce hydrogen gas and carbon monoxide. In a subsequent water-gas shift reaction, the carbon monoxide is further reacted with steam to produce carbon dioxide and additional hydrogen gas. The hydrogen gas is subsequently separated from the carbon dioxide through pressure swing adsorption, membrane separation, or another gas separation process. Thus, most hydrogen that is produced in refinery operations, for example, produces greenhouse gases, which must be captured and sequestered to yield meaningful benefit.\|[0005] Alternatively, hydrogen gas may be generated by the electrolysis of water into hydrogen gas and oxygen. The hydrogen gas is subsequently separated from oxygen through pressure swing adsorption, membrane separation, or another gas separation process. Hydrogen production via electrolysis, or partial pyrolysis reactions, requires a substantial amount of electricity. While at least some of the required electricity for hydrogen production via electrolysis and/or partial pyrolysis reactions may be obtained from renewable sources (e.g., wind, solar, and hydroelectric), in practice the majority of the electricity used for this purpose has traditionally been, and continues to be, produced through the combustion of fossils fuels, which also produces greenhouse gases.\|[0006] The abiotic production of hydrogen gas is known to occur in certain geological formations, e.g., at young oceanic crust near a mid-oceanic ridge, as depicted in FIGS. 1A-1D. These natural reactions occur across a range of environmental conditions that include variable pH, oxygen fugacity, chemical composition, and pressure. Such reactions produce variable and complex mineralogy and chemistry but do not predictably produce any specific combination of reaction products. In fact, as generally illustrated in the cross-section photograph of FIG. 2, rock deposits 200 that may yield abiotic hydrogen often contain complex mixtures or layers of difficult-to-extract mineral phases, or will not produce a desired product if other competing reactions are preferred based on in situ geochemical conditions (e.g., variable redox potential (Eh), pH, pore water composition, gas chemical composition, and temperature). For example, hydrogen production is highly variable in nature and its occurrence greatly depends on pH, Eh, and other aspects of fluid geochemistry in pore spaces and at mineral surfaces. Thus, the complex kinetics of reaction phases and the occurrence of competing reactions in natural conditions (e.g., circumneutral pH, variable oxygen fugacity, and variable pore water chemistry) govern the products yielded by these naturally occurring reactions. Certain geological formations and/or the rocks thereof are also known to contain minerals that are conducive to reaction with carbon dioxide under certain conditions to form carbonated mineral phases, e.g., carbonates.\|BRIEF SUMMARY\|[0007] FIG. 3 provides a map that highlights the example locations of selected suitable and/or robust deposits of mafic and ultramafic rock around the world. Olivine- and pyroxene-bearing ores may be found in such mafic and/or ultramafic formations. As can be understood from FIG. 3, sources of mafic and ultramafic igneous rocks may be found in many locations and are quite plentiful, accounting for at least 10% of the continental crust of the Earth, which illustrates the global applicability of solutions described herein. More recently, such sources of mafic and ultramafic igneous rock have garnered interest for their potential exploitation to sequester (mineralize) carbon dioxide in carbonate mineral phases. However, despite significant prior work on carbon sequestration, there is considerable debate about the best mechanistic reactions and optimized rates for carbon mineralization. As such, the economic viability of these processes has not been fully developed, nor has the hydrogen generation and carbon sequestration capacity of mafic and ultramafic rocks been realized. Moreover, no economic use has been identified for the fine-grained carbonated mineral phases that result from carbonization reactions. Rather, proposals have recommended such carbonated mineral phases be used as fill or dumped in oceans or lakes).\|[0008] Despite the theoretical potential for such geological formations and/or the ores thereof to be exploited for geological hydrogen or other products, and for potential carbon sequestration, the processes and kinetics of these reactions has not been rigorously evaluated nor optimized. Further, processes for the production of hydrogen from these geological formations without the occurrence of alternative, and sometimes deleterious, mineral phases (e.g., serpentine, such as antigorite, asbestos) have not been developed. Accordingly, Applicant has recognized a need for systems and methods that exploit certain geological formations and/or the ores thereof to liberate hydrogen, generate magnetite and magnesite, and/or derive other desired products, such as scarce/critical metals from geological formations that include olivine- and pyroxene-rich ores, and in addition, sequester carbon dioxide in magnesite or other mineral phases.\|[0009] The disclosure herein provides one or more embodiments of systems and methods for sequestering carbon, evolving hydrogen gas, and producing magnetite as well as magnesite from olivine- and pyroxene-bearing ores. In addition, precious or scarce metals, such as nickel, cobalt, chromium, and rare earth elements, may be concentrated in the remaining ore, which facilitates their recovery.\|[0010] In an example embodiment, a method is provided for sequestering carbon and producing hydrogen and magnetite. The method includes obtaining an ore that containing olivine or pyroxene. The ore may be comminuted into smaller size fractions, such as by crushing or grinding. The comminuted ore may be introduced into a reactor that is operable at temperatures above ambient temperature and pressures above atmospheric pressure. The method may also include introducing carbon dioxide (or a mixture of carbon dioxide and other gases such as nitrogen (N2), dihydrogen sulfide (H2S), and sulfur dioxide (SO2) into the reactor at a first temperature above ambient temperature for a first residence time to react at least a portion of the carbon dioxide with the ore. The method also includes later introducing water into the reactor at a second temperature for a second residence time to react at least a portion of the water with one or more of the remaining ore to generate at least magnetite and hydrogen gas. Reaction products, including hydrogen gas, magnesium carbonate (magnesite), magnetite, other reaction products, and any remaining ore may be removed from the reactor.\|[0011] In another embodiment, a method is provided for sequestering carbon and generating hydrogen and magnetite from rock. The method includes obtaining an ore that olivine or pyroxene. As above, the ore may be broken down into smaller size fractions, such as by crushing or grinding. The ore is introduced into a first reactor that is operable at a first temperature above ambient temperature and pressures above atmospheric pressure. The method also includes introducing carbon dioxide (or a mixture of carbon dioxide and other gases such as nitrogen (N2), dihydrogen sulfide (H2S), and sulfur dioxide (SO2)) into the first reactor at the first temperature for a first residence time to react at least a portion of the carbon dioxide with the ore to generate at least magnesium carbonate. The remaining ore may be passed to a second reactor. Reaction products from the first reactor may be separated from the remaining ore or may also be passed to the second reactor. The method also includes introducing water into the second reactor at a second temperature for a second residence time to react at least a portion of the water with the remaining ore in the second reactor to produce at least magnetite and hydrogen gas. Reaction products, including hydrogen gas, magnesium carbonate (magnesite), magnetite, other reaction products and any remaining ore may be removed from the second reactor.\|[0012] In yet another embodiment, a system is provided for sequestering carbon and producing hydrogen and magnetite from rock. The system includes a source of ore that contains olivine or pyroxene. The system may include a crusher or grinder used to physically reduce the particle size of the ore introduced therein from the source. The system may include a sieve used to receive the ore from the crusher and configured to allow ore particles up to a pre-selected size to pass therethrough. The system also includes a reactor having an inlet that receives ore particles up to the pre-selected size from the sieve and at least one outlet. The reactor also has at least one additional inlet through which one or more of carbon dioxide or water may be introduced (and in some embodiments, the reactor may comprise two reactors: a first reactor having an additional inlet through which carbon dioxide may be introduced, and a second reactor having another additional inlet through which water may be introduced). The reactor is operable at a first temperature for a first residence time to react at least a portion of any received carbon dioxide with the ore in the first reactor to generate at least magnesium carbonate. The reactor is also operable at a second temperature for a second residence time to react at least a portion of any water that enters the reactor through the at least one additional inlet with any ore within the reactor to generate magnetite and hydrogen gas. In one or more embodiments, the system also includes a gas separator that is connected to and in fluid communication with the at least one outlet of the reactor. The gas separator is configured to separate hydrogen gas from gases that exit the reactor through at least one outlet of the reactor.\|[0013] Corresponding means for performing these various steps are set forth below.\|[0014] The foregoing brief summary is provided merely for purposes of summarizing some example embodiments described herein. Because the above-described embodiments are merely examples, they should not be construed to narrow the scope of this disclosure in any way. It will be appreciated that the scope of the present disclosure encompasses many potential embodiments in addition to those summarized above, some of which will be described in further detail below.\|(US12545576)\|BRIEF DESCRIPTION OF THE FIGURES\|[0015] Having described certain example embodiments in general terms above, reference will now be made to the accompanying drawings, which are not necessarily drawn to scale. Some embodiments may include fewer or more components than those shown in the figures.\|[0016] FIGS. 1A, 1B, 1C, and 1D illustrate cross-sectional representations of young oceanic crust and associated structures positioned near a theoretical mid-oceanic ridge that may produce and/or host abiotic hydrogen production.\|[0017] FIG. 2 illustrates an example cross-section of serpentinized ultramafic rock.\|[0018] FIG. 3 illustrates a map with locations of suitable olivine- and pyroxene-bearing localities throughout the world.\|[0019] FIG. 4A provides an example flow diagram illustrating a sequence of operations performed by a system to enhance carbon dioxide sequestration, hydrogen gas evolution, and magnetite and magnesite production using a single reactor, in accordance with some example embodiments described herein.\|[0020] FIG. 4B provides an example flow diagram illustrating a sequence of operations performed by a system to enhance carbon dioxide sequestration, hydrogen gas evolution, and magnetite/magnesite production using multiple reactors, in accordance with some example embodiments described herein.\|[0021] FIG. 5 illustrates an example flowchart for enhancing carbon dioxide sequestration, hydrogen gas evolution, and magnetite/magnesite production, in accordance with some example embodiments described herein.\|[0022] FIG. 6 illustrates an example flowchart for acquisition and preparation of source rock for reaction, in accordance with some example embodiments described herein.\|[0023] FIG. 7 illustrates an example flowchart for processing rock remaining following any carbon dioxide and/or water reactions, in accordance with some example embodiments described herein.\|(US12545576)\|DETAILED DESCRIPTION\|[0024] Some example embodiments will now be described more fully hereinafter with reference to the accompanying figures, in which some, but not necessarily all, embodiments are shown. Because inventions described herein may be embodied in many different forms, the invention should not be limited solely to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will satisfy applicable legal requirements.\|Overview\|[0025] Applicant recognized that despite the significant theoretical potential of mafic and/or ultramafic igneous rocks (or, more broadly, olivine- and pyroxene-bearing ores, such as those with elevated iron content), as described above, to serve as geological sources for economic geological hydrogen, to be exploited as natural sources and catalysts for hydrogen and magnetite production, and to be exploited for carbon sequestration, the optimal processes and kinetics for these reactions have not been rigorously evaluated nor optimized. Specifically, process steps to enhance both carbon sequestration and the production of hydrogen, magnetite, magnesite, and/or other minerals from these types of rocks—without the formation of alternative (and sometimes deleterious, e.g., serpentine, asbestos) mineral phases—have not been developed.\|[0026] Further, Applicant is unaware of any prior attempts to use an optimized chemical process of carbon mineralization to enhance the kinetics of hydrogen and magnetite production, or to regulate the chemical species of the resulting reaction products (e.g., prevent the formation of serpentine and asbestos).\|[0027] In various embodiments disclosed herein, carbon dioxide may be sequestered, and hydrogen, magnetite, and other scarce metals may be produced economically (and with a neutral to net-negative carbon footprint) using olivine- and pyroxene-rich ores through sequential carbonation and serpentinization reactions in a controlled environment. Thus, Applicant has developed an engineering process that employs sequential reactions to exploit the potential for olivine- and pyroxene-rich ores to both sequester carbon dioxide dominantly as magnesite or other carbonate minerals, as well as liberate hydrogen, magnetite, and/or other desirable minerals/scarce metals. Applicant further recognized that additional process steps applied to the olivine- and pyroxene-rich ores may enhance the concentration and recovery of precious or scarce metals (e.g., nickel, cobalt, chromium, lithium, and rare earth elements.), which are needed for renewable energy and energy storage, among other uses.\|[0028] Applicant discovered that the serpentinization reaction process can be advantaged such that the chemical activity and commensurate rates of reactions between water and fayalite and/or ferrosilite may be enhanced by first removing a significant component of forsterite from the olivine mineral phase and increasing the comminution of mineral grains by inducing the described chemical reactions. In this way, the fayalite and/or ferrosilite in the igneous rock is concentrated and/or becomes less obscured by adjacent minerals, e.g., forsterite. This process benefits the reaction in two ways: first, by enhancing the surface area of fayalite and/or ferrosilite exposed for the reaction; and second, by pre-concentrating the reactant (iron-rich olivine (fayalite) or pyroxene (ferrosilite)) of choice. Thus, in one or more embodiments, forsterite and/or enstatite are at least partially removed prior to reacting the fayalite and/or ferrosilite with water.\|[0029] Some primary differentiators that demonstrate the value of example ex situ engineered embodiments that produce hydrogen, magnesite, magnetite, and critical metals via this pathway include: 1) the immense geological scalability of such embodiments once the “serpentinization” processes are optimized to produce the desired products (hydrogen, magnetite, scarce metals), as opposed to alternative mineral phases such as serpentine, asbestos, etc.; 2) the potential to permanently and verifiably sequester CO2 in a mineralized form and hence produce hydrogen, magnetite, and scarce metals in a carbon-negative process; and 3) the price point of potentially scalable “green” or “golden” hydrogen (i.e., carbon negative hydrogen), magnetite, and scarce metals, which can be greatly offset by considering other values streams generated using the quarrying concept (i.e., the sale of aggregate or higher value utilization of magnesite).\|[0030] Although a high-level explanation of the operations of example embodiments has been provided above, specific details regarding the configuration of such example embodiments are provided below.\|Serpentinization and Carbonation Reactions\|[0031] The disclosure herein provides one or more embodiments of systems and methods that facilitate the production of hydrogen, magnetite, and/or other desired minerals through serpentinization reactions involving olivine- and pyroxene-rich ores generally found in mafic and/or ultramafic igneous rock, or of any other rock assemblages containing such olivine- and pyroxene-rich ores. Table 1, provided below, gives representative serpentinization reactions involving fayalite (Fe2SiO4) and/or ferrosilite (Fe2Si2O6). Fayalite is a mineral phase that is the iron-rich endmember of the olivine solid solution series and is abundant in olivine-rich orc. Ferrosilite is the iron-rich endmember of the orthopyroxene solid solution series and is associated with pyroxene-rich ore. Fayalite and ferrosilite are commonly found together in mafic and ultramafic igneous rocks. Under certain conditions, water reacts with fayalite and ferrosilite to generate magnetite (Fe3O4), silica (SiO2), and hydrogen gas (H2) in the appropriate stoichiometric ratios. In each case, two moles of hydrogen gas are produced from three moles of either fayalite or ferrosilite mineral.\|[0032] TABLE 1 Hydrogen-Generating Serpentinization ReactionsSerpentinization Reactions Moles of MineralSerpentinizationIgneousMolesMineralPhaseReactionMineralof H2 OlivineFayalite3 Fe2 + 2 H2O →32 2 Fe3O4 + 3 SiO2 + 2 H2 PyroxeneFerrosilite3 Fe2Si2O6 + 2 H2O →32 2 Fe3O4 + 6 SiO2 + 2 H2 \|[0033] In one or more embodiments, the disclosed systems and methods may also facilitate the sequestration of gaseous carbon dioxide as mineralized carbonates through carbonation reactions involving the magnesium-rich endmember of olivine- and pyroxene-rich ores found typically in mafic and/or ultramafic rock. Table 2, provided below, gives representative carbonation reactions involving forsterite (Mg2SiO4) and enstatite (Mg2Si2O6), as well as illustrating the potential for carbonation during reaction with antigorite (Mg3Si2O5(OH)4) that can be formed as an accessory mineral phase in natural systems in which fluid conditions are not idealized for the formation of magnesite. Forsterite is a mineral phase that is the magnesium-rich endmember of the olivine solid solution series associated with olivine-rich ore. Enstatite is a mineral phase that is the magnesium-rich endmember of the orthopyroxene solid solution series associated with pyroxene-rich ore. Antigorite is an example mineral phase that is associated with serpentine. Under certain conditions, carbon dioxide reacts with forsterite and enstatite, and/or other accessory mineral phases (e.g., antigorite) to generate at least magnesium carbonate (MgCO3) and silica (SiO2) in appropriate stoichiometric ratios. The reaction of antigorite with carbon dioxide further yields a stoichiometric quantity of water and is shown to illustrate serpentinization reactions that occur in natural systems in which pH, Eh, temperature, pressure, and fluid chemistry cannot be optimized. In the case of the idealized carbonization reaction involving forsterite and enstatite, two moles of carbon dioxide gas are converted to magnesium carbonate (magnesite) per mole of either forsterite or enstatite mineral.\|[0034] TABLE 2 Carbon-Sequestering Carbonation ReactionsDecarbonation Reactions Moles of MineralDecarbonationIgneousMolesMineralPhaseReactionMineralof CO2 OlivineForsteriteMg2SiO4 + 2 CO2 →12 2 MgCO3 + SiO2 PyroxeneEnstatiteMg2Si2O6 + 2 CO2 →12 2 MgCO3 + 2 SiO2 SerpentineAntigoriteMg3Si2O5(OH)4 +13 3 CO2 → 3 MgCO3 + 2 SiO2 + 2 H2O \|[0035] In nature, and as previously described, the above-described serpentinization and carbonization reactions occur, but only as a subset of a variety of reactions occurring across a range of environmental conditions in the subsurface or at surface conditions of the earth. As a result, the environmental conditions are often variable and reactions kinetics and pathways are far from ideal. Accordingly, natural reactions are based on the variable (and often dynamic, i.e., changing with time) pH, oxygen fugacity, temperature, pore water chemical composition, gas chemical composition, and pressure found in nature, specifically in the subsurface. The multitude of reactions and potential pathways for those reactions occurring in nature lead to the formation of variable and complex chemistry and assemblages of minerals, but do not predictably produce any specific combination of usable reaction products. Instead, natural systems, which evolve through time and under varying reaction conditions produce complex (and often heterogeneous) complexes of varying mineral assemblages and products of reactions that did not follow the idealized reactions described above, or are slower to reach thermodynamic equilibrium.\|[0036] With respect to olivine and pyroxene mineralogy and chemistry, olivine is a solid solution series (X2SiO4, where X═Mg2+ or Fe2+) between a magnesium silicate (forsterite) and an iron silicate (fayalite) and pyroxene (i.e., orthopyroxene) is a solid solution series (X2Si2O6, where X═Mg2+ or Fe2+) between a magnesium silicate (enstatite) and an iron silicate (ferrosilite). In the olivine-rich deposits of interest, fayalite and ferrosilite are usually the minor constituent and typically range in concentration from 6% to 20%, with the lower range concentrations appearing more commonly in nature. Consequently, the thermochemical activities of fayalite and ferrosilite are relatively low compared to those of the forsterite or enstatite, respectively. Thus, if the olivine or pyroxene obtained from a quarry is crushed and reacted with water at favorable reaction conditions (i.e., controlled for temperatures, pressures, Eh, pH, and fluid composition, then a serpentinization reaction will proceed at a relatively low rate due to relatively low thermochemical activity and commensurately low rates of reactions with fayalite or ferrosilite. Nevertheless, when completed, the reaction produces magnetite, silica, and hydrogen (from the reaction of fayalite or ferrosilite with water) may be separated (magnetically or gravimetrically) from forsterite, enstatite, or magnesite. The mixture of olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite) minerals, however, constitutes an almost an “ideal” mixture that is exceedingly rare in natural systems. However, in an ideal mixture, the chemical activity varies linearly with the mole fraction and is roughly equal to the mole fraction. Thus, the chemical activity and reaction rate can be enhanced by pre-concentrating the abundance of olivine and pyroxene from the bulk ore and specifically the abundance of the iron-rich endmembers of both the olivine and pyroxene solid solution series.\|Ex Situ Sequestration of Carbon Dioxide and Generation of Hydrogen\|[0037] In various embodiments contemplated herein, carbon dioxide may be mineralized, and hydrogen, magnesite, magnetite, and critical metals may be produced economically (and with an overall neutral to net-negative carbon footprint) by an engineered system that causes sequential reactions in the manner shown in the flow diagrams illustrated in FIGS. 4A, 4B, and described in connection with the flowcharts provided in FIGS. 5, 6, and 7.\|[0038] FIG. 4A illustrates a flow diagram of one embodiment 400′ of a system for enhancing the production of hydrogen gas and magnetite from rock that contains a mixture of olivine (e.g., fayalite and forsterite) and pyroxene (e.g., ferrosilite and enstatite) minerals. A source of olivine- and/or pyroxene-rich ores 402 may be fed or introduced into a crusher or grinder 406 that reduces the size of the received ore into smaller size fractions. In one or more embodiments, a washer 404 may optionally be used to wash the ore with water or a mildly acidic solution to remove any contaminants therefrom and prepare the ore for carbonation reactions. The crushed or ground rock is then introduced into a sieve 408 or other such separator that segregates the rock into pre-selected particle ranges. In one or more embodiments, the sieves or grates thereof are sized to pass 150-, 80-, and even 45-micron grains, although different sizing can be utilized. In at least one embodiment, the comminuted rock is a powder or has a powder-like particle size range. Rock that does not pass through the sieve may be returned to the crusher or grinder 406 via a recycle loop 410 to be reduced further in size. The subset of the rock having particles within a pre-selected particle range of the sieve 408, e.g., 150-micron, 80-micron, 45-micron, or any size therebetween, is then fed or introduced into a reactor 412.\|[0039] The reactor 412 may be a rotary kiln, a toroidal fluidized bed, a fluidized bed, or another reactor known to those skilled in the art. The reactor 412 may have an inlet that receives ore (or ore particles) at least one outlet, from which any remaining ore may be removed following reaction within the reactor 412. The reactor 412 may further have at least one additional inlet through which one or more of carbon dioxide or water can be introduced into the reactor 412. The reactor 412 may be operable at a first temperature for a first residence time to react carbon dioxide that enters the reactor 412 through the at least one additional inlet with ore disposed within the reactor 412 to generate magnesium carbonate. The reactor 412 may further be operable at a second temperature for a second residence time to react water that enters the reactor through the at least one additional inlet (which may be the same inlet by which carbon dioxide enters the reactor 412 or a different inlet) with ore disposed within the reactor 412 to generate magnetite and hydrogen gas.\|[0040] In a first reaction step, carbon dioxide is introduced into reactor 412 with the crushed/ground rock. Water (approximately 10 liters of water per kilogram) may be applied (sprayed or washed) to the crushed/ground rock by washer 404 either before or after placement of the rock into the reactor 412. The wetting of the powdered rock with water allows for the dissolution of gaseous CO2 to carbonic acid (H2CO3) on the wet surfaces of the mineral grains, which enhances the reactivity of the carbon dioxide with the forsterite mineral found therein. In at least one embodiment, the pH of the water applied to the comminuted rock may be between about 4.8 to about 6.5. Water in this pre-selected pH range further enhances the reaction between the carbon dioxide and the forsterite mineral. During this first reaction step, the reactor is operated at a pre-selected temperature (>90° C.) and pressure (greater than approximately five bars) to facilitate the carbonation reaction with respect to the forsterite mineral found in the rock. In one or more embodiments, the reactor 412 is operated at a temperature of between about 100° C. to about 400° C. and at a pressure of between about five and up to at least 100 bars (e.g., about 40, 50, 75 or even 100 bars); note the upper limit of pressure can be extended to considerably higher pressures if the reactor 412 and associated components are able to withstand such pressures. Increasing pressure in this fashion will produce a corresponding enhancement of the carbonation reaction being prompted at this stage of the process. In other embodiments, the operating pressure of the reactor 412 may be as low as 35 bars, as low as 30 bars, as low as 25 bars, as low as 20 bars, as low as 15 bars, as low as 10 bars, as low as 5 bars, or even lower (˜1 bar), and may still prompt the intended carbonation reactions, albeit at commensurately lower rates of reaction. As provided in Table 2 above, the reaction of carbon dioxide with the forsterite (Mg2SiO4) produces magnesium carbonate (MgCO3) and silicon dioxide (SiO2) as reaction products. In this way, the forsterite mineral of the mafic and/or ultramafic rock is used to permanently sequester CO2 in the form of an insoluble magnesium carbonate mineral lattice, which is a solid that that can be useful as a raw material, placed in a landfill, ocean, lake, or otherwise easily stored. By reacting the crushed/ground rock containing the forsterite with carbon dioxide at favorable conditions of temperature, pressure, Eh, and pH, the forsterite can be altered to magnesite following reaction with carbon dioxide.\|[0041] It will be understood that, although this first reaction step favorably enhances the comminution of source rock and better prepares any remaining rock for the second reaction step described below, some embodiments may not perform this first reaction step, and instead may simply comminute the source rock, which itself prepares the source rock for the second reaction step, as illustrated by way of example in the Example Implementation section below. Of course, in other embodiments, the source rock may not need to undergo an initial comminution step, but may instead simply be initially processed using the first reaction step described herein, which itself fosters comminution of the source rock and thus prepares it for more effective reaction in the second reaction step described below. Both comminution of the source rock and the carbonation reactions occurring during the first reaction step favorably dispose any remaining rock for the section reaction step below; accordingly, various combination of comminution and the first reaction step may be employed in various scenarios based on the desired results of a given implementation.\|[0042] In a second reaction step, water is thereafter introduced into reactor 412 with the crushed/ground rock, which may in some embodiments still contain the magnesium carbonate and silicon dioxide from the first reaction step, the fayalite and/or ferrosilite minerals in the original crushed/ground rock, and any other minerals/ores found in the original crushed/ground rock. In some embodiments, magnesium carbonate and silicon dioxide from the first reaction step can be separated from the residual iron silicate phases based on their respective densities. In one or more embodiments of these processes, the water that is added to the reactor 412 may have a low oxygen fugacity (e.g., it may be obtained from municipal wastewater treatment, groundwater, geothermal water, mine waters, another industrial water source, or by reacting a municipal water (i.e., “tap water”) over a bed of copper at temperatures exceeding 125° C., or by another mechanism) and a pH of between about 8.3 and about 11.1 (with the specified pH being artificially attained, such as by adding sodium bicarbonate to the water, or naturally obtained, such as where the water with such pH range may be found in certain sources of water and wastewater). During this second reaction step, the reactor is operated at a pre-selected temperature and pressure (˜1 to 20 bars) to facilitate the serpentinization of the fayalite and/or ferrosilite minerals in the rock. In one or more embodiments, the reactor 412 is operated at a temperature in the range of between about 80° C. and about 400° C. As provided in Table 1 above, the reaction of water with the fayalite (Fe2SiO4) and/or ferrosilite (Fe2Si2O6) produces hydrogen gas, variable mixtures of nitrogen (N2), carbon dioxide (CO2), silicon dioxide, and magnetite (Fe3O4) as reaction products. The molecular and isotopic composition of hydrogen formed during this ex situ process will be determined by the temperature conditions of the reaction (e.g., ˜175° C.) and the composition of the initial water, wherein the fractionation factors (a) between H2O and H2 follow the fractionation factors observed for standard geothermometers. The hydrogen gas, along with any other gases in the reactor 412, such as unreacted carbon dioxide (CO2), sulfur dioxide (SO2), or dihydrogen sulfide (H2S) or inert gases (e.g., nitrogen (N2), argon (Ar) from the first reaction step, are passed to a gas separator 414. The gas separator 414 may be a membrane unit, a pressure swing adsorption, or a cryogenic separation unit that can separate the hydrogen gas from other gases, e.g., atmospheric gases, that may also be present in the reactor 412. The gas separator 414 may be connected to and in fluid communication with at least one outlet of the reactor 412 and configured to separate hydrogen gas from gases that exit the reactor 412 through the at least one outlet.\|[0043] In at least one embodiment, gases that may be present in the reactor 412 prior to the second reaction may be evacuated prior to the second reaction, such as by pulling a vacuum on the reactor 412. Without these contaminant gases in the reactor 412 (e.g., N2 or CO2), the hydrogen gas that is formed as a result of the serpentinization reaction with water may be the only gas present after the second reaction step. In such case, the gas separator 414 may not be needed to segregate the hydrogen gas as a product. After the second reaction step, the magnesium carbonate, silicon dioxide, magnetite, and any remaining rock/unreacted ore may be removed from the reactor 412. In some embodiments, magnesium carbonate (i.e., magnesite) and silicon dioxide (i.e., quartz) may be separated from iron silicates and other mineral phases before the material is placed in reactor 412. The magnetite, which represents a valuable product/feedstock for the iron industry (with particular value in direct reduced iron manufacturing), may be recovered from the magnesium carbonate, silicon dioxide and any remaining rock/ore by, for example, magnetic separation or other density separation techniques. A magnetic separator 416 may be used to selectively attract the magnetite through the use of one or more magnets and thereby physically remove the magnetite from the other non-metallic ore. In one or more embodiments, the solid products, e.g., the magnetite, magnesium carbonate, silicon dioxide, and any remaining, unreacted ore/rock may be further crushed or ground (not shown in FIG. 4A) to facilitate the removal of magnetite particles from the other solids in the magnetic separator 416 or conduct secondary recovery of other minerals or metal-rich phases. The separated hydrogen gas from gas separator 414 and the magnetite recovered via the magnetic separator 416 are valuable products whose production and recovery from mafic and/or ultramafic rock are enhanced by the disclosed sequential carbonization and serpentinization reactions disclosed herein.\|[0044] The remaining magnesium carbonate (in which the carbon is permanently sequestered in the mineral phase), silicon dioxide, and any unreacted rock/ore may be used as an aggregate material and/or placed in landfill or otherwise disposed of. In one or more embodiments, the magnesium carbonate and silicon dioxide may be separated (based on density separation techniques such as heavy liquids or other gravity separation, or sluicing) and removed from the remaining rock/gangue (gangue: collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) materials. As further discussed below, magnesium carbonate (or magnesite) is useful in the manufacturing of pharmaceuticals, agricultural lime, and fertilizers (to neutralize acidification caused by fertilizer use), ceramics and ceramic brick, and as flux used in iron and steel manufacturing. Magnesite may also be used as a partial lime substitute to enable lower carbon emissions that result from the lower temperatures required to make magnesium oxide (MgO) as compared to calcium oxide (CaO) for cement manufacturing. Further, magnesite can be used as a carbon negative concrete filler and cement or aggregate substitute in concrete.\|[0045] In one or more embodiments, rather than landfilling or otherwise using the bulk of the magnesium carbonate, silicon dioxide, and any unreacted rock/ore, the rock and/or gangue material from the first reaction phase is further processed to separate and remove specific valuable components therefrom. For example, elevated concentrations of certain precious metals (e.g., nickel, cobalt, chromium, and rare earth elements) in mafic and ultramafic rocks are further concentrated in this “slag” material. In at least one embodiment, highly elevated metal enrichments, that include but are not limited to phosphates, aluminum oxides, precious metals, and other mineral gangue may be separated from the remaining rock/ore by, for instance, heavy liquid separation or other gravity separation, or sluicing in a separator 418. Through gravity separation, the various metals and other valuable components are ground into fine particles and separated based on their individual specific weights.\|[0046] As illustrated in FIG. 4A, the first and second reactions can both occur in the same reactor 412, which may be a rotary kiln, fluidized bed, toroidal bed, or other reactor as described previously, in which case the reactions may be run sequentially, and all products separated at the completion of both reactions. In one or more embodiments (not shown in FIG. 4A), the reaction products (i.e., magnesium carbonate and silicon dioxide) may be separated after the first reaction step and prior to the second reaction step using established density separation techniques such as heavy liquid separation or other gravity separation, or sluicing. In other embodiments, as shown in FIG. 4A, the reaction products remain in the reactor during the second reaction step. Even if the reaction products are not physically separated, the thermochemical activity and reaction rates of fayalite and/or ferrosilite will increase according to the newly exposed surface area of fayalite and/or ferrosilite minerals. In other words, the reactivity of the serpentinization reactions with respect to the fayalite and/or ferrosilite minerals will proceed according to the now higher molar fraction of fayalite and/or ferrosilite in the solid solution (i.e., the number and/or extent of alternative side reactions has been reduced). With respect to the upper limit of the fully separated (e.g., using established density separation techniques such as heavy liquid separation or other gravity separation, or sluicing) or exposed fayalite and/or ferrosilite, the thermochemical activity of the powdered material should approach unity of the pure phase mineral, or mixtures of fayalite and/or ferrosilite mineral phases. Thus, the first reaction step involving the reaction of the forsterite with carbon dioxide increases the thermochemical driver for the second reaction step, which is the serpentinization/hydration reaction of the fayalite and/or ferrosilite with water, by reducing the availability of forsterite and increasing the exposed surface area of fayalite and/or ferrosilite minerals. The former increases the kinetic rate by driving the thermochemical activity toward that of a pure compound, while the latter enhances chemical activity by increasing the surface area available for reaction.\|[0047] FIG. 4B illustrates a flow diagram of another embodiment 400″ of a system of enhancing the production of hydrogen gas and magnetite from a source rock that contains a mixture including olivine (fayalite and forsterite) and/or pyroxene (ferrosilite and enstatite) minerals. The flow diagram of FIG. 4B is similar to that of FIG. 4A, except that the first reaction step occurs in a first reactor 412′ and the second reaction step occurs in a second reactor 412″. The first reactor 412′ facilities the carbonation reaction between the forsterite mineral and carbon dioxide. The crushed/ground ore of a uniform or pre-selected particle size range is passed from the sieve 408 or other particle size separator into the first reactor 412′. Carbon dioxide is pumped into the first reactor 412′ in above stoichiometric ratios to facilitate the carbonization reactions listed in Table 2. After the first reaction has occurred, the magnesium carbonate and silicon dioxide products, along with the unreacted fayalite and/or ferrosilite, and other remaining ore, are passed to the second reactor 412″.\|[0048] Continuing with FIG. 4B, the second reactor 412″ facilitates the serpentinization reaction between the fayalite and/or ferrosilite mineral phases and water (or steam). The reaction products and remaining rock/ore from the first reactor 412′ are introduced into the second reactor 412″. Water is pumped into the second reactor 412″ in above stoichiometric ratios (>˜20 liters/kg of rock) to facilitate the serpentinization reactions listed in Table 1. After the second reaction has occurred, the reactor gases, including the hydrogen gas evolved during the second reaction step, are passed or routed to a gas separator 414, as described above with respect to FIG. 4A. Likewise, the solid reaction products, including magnesium carbonate, silicon dioxide, magnetite, as well as any unreacted ore/rock are passed to a magnetic separator 416, as described above with respect to FIG. 4B. Other than the use of two reactors 412′ and 412″ in place of one reactor 412, as described above, the embodiments represented by FIGS. 4A and 4B are similar. It should be noted that the configuration of the system of FIG. 4B provides a semi-continuous method in that the separate process vessels, e.g., reactors 412′ and 412″, are dedicated to differing portions of the method.\|[0049] FIGS. 5, 6, and 7 illustrate flowcharts of various embodiments for enhancing the production of hydrogen gas, magnetite, magnesite, and scarce metal resources from mafic and ultramafic igneous rock that contains a mixture of olivine (fayalite and forsterite) and pyroxene (ferrosilite and enstatite) minerals. As previously disclosed in connection with FIG. 3, olivine- and/or pyroxene-rich ores may be found in numerous locations around the world. At block 502, such olivine- and/or pyroxene-rich ore may be acquired from geological sites containing high concentrations of such rocks in one or more of these areas. FIG. 6 illustrates this rock acquisition operation in greater detail. As shown at block 602, the olivine- and/or pyroxene-rich source rock may be acquired in any manner known to those skilled in the art, such as by underground mining, strip mining, quarrying, outcrop quarrying, or the use of waste (i.e., mine tailings), etc. The source rock may be transported, e.g., by barge, train, truck, etc., to a facility to further process the rock. In one or more embodiments, the source rock may be processed in proximity to the location where the rock is acquired. The source rock may be processed by crushing and/or grinding the rock at block 606 into smaller size fractions. In addition to creating uniform or near uniform sizing, such comminution also helps to expose the minerals, such as olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite), that are contained within the rock. If the rock is processed in proximity to the geological site from which the rock originated, then the processed rock may then be transported to a facility having a system to further extract hydrogen, magnetite, and other valuable products from the ore according to a method disclosed herein (not shown in FIGS. 5 and 6). At block 608, the crushed and/or ground source rock may be further processed by sieving or otherwise segregating the rock according to size. In one or more embodiments, the crushed and/or ground rock may be washed with water or a slightly acidic solution to clean the surfaces thereof of dust, dirt, or other contaminants. As illustrated at block 604, such washing may be conducted before the rock is crushed and/or ground and can also benefit from agitation.\|[0050] The crushed and/or ground rock is then introduced into a reactor at block 610 in which the rock is reacted with carbon dioxide and water to produce magnesium carbonate and hydrogen gas, among other products, in stoichiometric proportions via the carbonation reactions described in Table 2. The crushed/ground rock may be transported between and introduced into the reactor at block 610 by conveyor, by machinery placement, etc. A slightly acidic water solution, as previously described may be applied, e.g., by washing, spraying, or soaking, onto the outer surfaces of the rock. Such application may be before or after the rock is deposited in the reactor. The air in the reactor, including oxygen therein, may be evacuated from the sealed reactor with the rock disposed therein (e.g., by applying a vacuum to the reactor) or purged using reaction gas (e.g., N2) prior to commencing the reaction. Returning to FIG. 5, block 504 describes that carbon dioxide (CO2) is introduced into the reactor to begin the first reaction phase. The carbon dioxide may be gaseous or supercritical as previously described. A greater-than-stoichiometric portion of carbon dioxide is added as compared to the amount of rock (and specifically forsterite concentration therein) in the reactor in order to ensure that the carbon dioxide does not limit the carbonation reaction and to benefit from increased reactivity that is observed to occur at elevated pressures of CO2 and/or super-critical CO2. At block 504, the reactor is operated at one or more pre-selected temperatures and pressures, as described above, for a first residence time in order to sufficiently react the carbon dioxide with the forsterite mineral to produce magnesium carbonate and silicon dioxide reaction products. At the end of the first residence time, the gas phase from the reactor may be evacuated by, e.g., applying a vacuum or gas purging operation, to remove the excess unreacted carbon dioxide and any other gases evolved via the carbonation reactions of the first reaction phase.\|[0051] Continuing with FIG. 5, at block 506, water is introduced to the reactor after the first residence time. In one or more embodiments, the water is a low oxygen fugacity water that is prepared or obtained as described in greater detail above. Again, a greater-than-stoichiometric portion of water (>˜20 liters/kg of rock) is added as compared to the amount of rock (and specifically fayalite and/or ferrosilite concentrations therein) in the reactor in order to ensure that the water does not limit the serpentinization reaction. At block 506, the reactor is operated at one or more pre-selected temperatures and pressures, as described above, for a second residence time in order to sufficiently react the water with the fayalite and/or ferrosilite minerals (now having additional exposed surface area and more optimized chemical activity due to the first reaction phase) to produce at least hydrogen gas and magnetite reaction products.\|[0052] At block 508, the gas phase is removed from the reactor either during or at the completion of the second reaction phase. This gas phase, which is rich in hydrogen gas (and may contain small quantities of trace gases, e.g., N2, Ar, CO2) may be further purified through gas separator 414 (as shown in FIG. 4A and FIG. 4B). The gas separator 414 may be a pressure swing adsorption unit, a membrane separation unit, a cryogenic separation unit, or any other gas separation unit known to those skilled in the art. If the gas phase was not evacuated from the reactor between the first reaction phase and the second reaction phase, then some carbon dioxide and/or other gases, e.g., reaction gases, may contaminate the hydrogen gas evolved in the reactor via the serpentinization reactions of the second reaction phase.\|[0053] At block 510, the remaining rock within the reactor may be further processed to remove the magnesium carbonate/magnesite, the iron oxide/magnetite, the silicon dioxide, any remaining ore and/or slag material from the reactor. These operations are described in detail in connection with FIG. 7. Block 702 illustrates that the remaining rock in the reactor may be removed for further processing. Such removal may include removal by mechanical machinery, which picks up, rakes, or gravity feeds the material from the reactor into a container or onto a conveyor. In particular, at block 702 the solid reaction products (i.e., magnesite, magnetite, etc.), the remaining ore, and any slag material may be passed to a magnetic separator 416 (as shown in FIG. 4A and FIG. 4B) in order to separate the magnetite from the other materials via attraction of the magnetically susceptible iron oxide to a magnetic field (see block 704). The solid material removed from the reactor at block 702 may undergo additional crushing and/or grinding in order to create a fine powder to facilitate removal of valuable components thereof (not shown in FIGS. 5 and 7). At block 706, any precious or scarce metals that are now more concentrated in the remaining ore and/or gangue (collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) material after magnetite removal may be separated and removed based on density separation techniques such as heavy liquid separation or other gravity separation, or sluicing; an example of gravity separation using a gravity separator is shown in 480. Finally, as shown in block 708, the remaining rock, containing remaining magnesium carbonate (in which the carbon is permanently sequestered in the mineral phase), silicon dioxide, and any unreacted rock/ore may be used as an aggregate material and/or placed in landfill or otherwise disposed of. As noted previously, in some embodiments the magnesium carbonate and silicon dioxide may be separated (based on density separation techniques such as heavy liquids separation, or other gravity separation, or sluicing) and removed from the remaining rock/gangue (gangue: collection of accessory mineral phases such as phosphates, sulfides, aluminum oxides, etc.) materials for separate dispositioning.\|[0054] FIGS. 5, 6, and 7 illustrates operations performed in various example embodiments. It will be understood that each flowchart block, and each combination of flowchart blocks, may be implemented by various means. The flowchart blocks support combinations of means for performing the specified functions and combinations of operations for performing the specified functions. In some embodiments, some of the operations above may be modified or further amplified. Furthermore, in some embodiments, additional optional operations may be included. Modifications, amplifications, or additions to the operations above may be performed in any order and in any combination.\|(US12545576)\|Example Implementation\|[0055] In one example embodiment, an ultramafic ore was reacted with carbon dioxide to sequester the carbon in the magnesium carbonate mineral phase and water to evolve hydrogen gas as well as produce magnetite. The example was conducted in three phases: 1) rock preparation; 2) water preparation; and 3) reaction process, each of which will be described in greater detail below. As part of the analysis of the overall system and method, the composition of the ore (i.e., olivine (forsterite and fayalite) and pyroxene (enstatite and ferrosilite) minerals), the reaction conditions to which the ore was subjected, and the characteristics of the carbonation/serpentinization reaction products were assessed. For instance, with respect to the ore composition, the mass, mineralogy, and geochemical composition of the bulk rock were evaluated by optical mineralogy, x-ray powder diffraction (XRD), and inductively coupled plasma mass spectrometry (ICP-MS) to evaluate the abundance of relevant constituents (e.g., fayalite, ferrosilite, FeO, MgO).\|[0056] In the rock preparation phase, an ultramafic aggregate material that included mostly rock particles of approximately 1 cm in size were collected from four active quarries (namely, two quarries in Pennsylvania, one in Virginia, and one in Kentucky). The ultramafic aggregate material was disaggregated (i.e., lightly crushed/comminuted) initially with a rock hammer and then with a Spex Ball mill. The powdered material was then sieved using grates arranged and designed to pass 150-, 80-, and then 45-micron grains successively. This enabled experimentation to be conducted on at least three different grains sizes. Another material—a homogenized olivine mineral—was also purchased from a scientific supplier in California. This olivine material, which was homogenized for size and composition, had a uniform particle size of approximately 100 microns.\|[0057] In the water preparation phase, three preparations were made. First, a low oxygen fugacity, high pH water was obtained by adding sodium bicarbonate and/or either sodium or potassium hydroxide to tap water in order to adjust the pH of the water to three levels 8.3, 9.7, and 11.1. As understood by those skilled in the art, oxygen fugacity (fO2) is a measure of the amount of oxygen available to react with elements having multiple valence states—such as iron and carbon. A high oxygen fugacity is indicative of a high chemical potential of oxygen in the water. A lowered oxygen fugacity of water can be achieved or in a variety of manners (e.g., by the use of low oxygen fugacity water supply such as municipal wastewater, groundwater, mine water, or other wastewater stream). One method for simply and reliably generating low oxygen fugacity water utilizes a heated bed of copper filings at 125° C. through which the water is passed to reduce the oxygen fugacity of the water (i.e., decrease the amount of reactive oxygen in the water). Such a method was used in this example implementation. Second, a saline water was obtained by adding salt (sodium chloride) to tap water to create saline solutions ranging from 0.1 to 4.5 per mil. In preparation for carbon mineralization experiments, the pH of the saline water was adjusted to be between about 4.8 and about 6.5 using dilute HCl in a mixture of distilled water and a sodium acetate buffer.\|[0058] For the reaction process, a single batch reactor (made of 316 stainless steel) was designed and built to conduct the carbonation and serpentinization reactions in both batch and sequential configurations. All of the reactions were performed in this closed stainless steel reaction vessel as a “batch” reaction (i.e., closed system) with the exception of a fluid sampling port that was opened periodically. For each experiment, whole samples (approximately 250 grams) were selected and sliced into two equally sliced approximately 125 grams of raw material and then placed in the gas-tight, stainless steel reaction vessels. In preparation for the introduction of carbon dioxide to the vessel, distilled water was lightly acidified using dilute hydrochloric acid and a sodium acetate buffer, and then mixed with salt (sodium chloride) to create a 0.1 to 4.5 per mil NaCl saline solution at ambient oxygen fugacity. This prepared water solution was then sprayed onto the powdered rock introduced into the reactor vessel. The prepared water solution provided a wet surface that enhanced the carbon dioxide reactivity with forsterite during the subsequent carbonation reactions.\|[0059] In the first reaction phase, sequestration of carbon dioxide was targeted through carbonation reactions between the introduced carbon dioxide and the forsterite (and enstatite) in the ore. The acidic, saline water, prepared as described above, was applied to the powdered rock containing the forsterite mineral prior to placing the wetted (i.e., sprayed with water solution as described above) powdered rock into the stainless-steel reaction vessel. Before the introduction of carbon dioxide, the reactor vessel was evacuated using a mechanical rough pump to apply a vacuum and remove air from the reactor vessel, including ambient oxygen. Other embodiments involve flushing the vessel with inert gas (e.g., N2) or reaction gas (e.g., CO2 or mixtures thereof) to remove air.\|[0060] Next, either carbon dioxide gas or mixtures of carbon dioxide gas, e.g., in a 4:1 ratio of carbon dioxide to nitrogen gas mixture, was introduced at room temperature and at an initial pressure of two bars (i.e., twice atmospheric pressure); in another embodiment of this disclosure, other ratios of CO2 to N2 can be utilized. The carbon dioxide used was an ultra-high purity carbon dioxide, such that the purity of carbon dioxide in the gas was greater than 99.9%, although mixtures with lower purity CO2 can be utilized in various embodiments. The temperature inside the reactor vessel was then increased to 100° C., 150° C., 200° C., 250° C., 300° C., and 400° C. with the temperature being controlled by an external band heater and measured with a standard Omega K-wire thermocouple. At each temperature, the gas phase pressure was measured via the sampling port using a standard Omega 0 to 100 psi pressure gauge. At each temperature, an aliquot of gas measured using a Stanford Research Systems residual gas analyzer (“quadrupole mass spectrometer”) and SRI gas chromatograph fitted with a thermocouple detector. The total pressure of hydrogen was calculated by determining the product of the percentage of hydrogen gas measured using the residual gas analyzer and/or gas chromatograph with the pressure compared to atmospheric pressure and assuming PV=nRT.\|[0061] The kinetic rate of carbon mineralization appeared to increase by ˜1.6 times when temperatures increased from 150° C. to 300° C., but additional increases in the rate of CO2 mineralization were not statistically significant between 300° C. and 400° C. over reaction times of ˜18 hours in the batch experiments. Next, while holding a constant temperature of 250° C., the pressure was increased to 5, 10, 25, and 50 bars of carbon dioxide. At each step, the gas phase pressure via the sampling port was monitored using a standard Omega 0 to 100 psi pressure gauge on an attached expansion volume (to ensure the sample pressure was in the range of the available pressure gauge). For each pressure, an aliquot of gas was also measured using an SRS quadrupole mass spectrometer and SRI gas chromatograph fitted with a thermocouple detector after pressure reduction by expansion to a pre-evacuated sample chamber via the sampling port. The rate of carbon mineralization appears to increase by ˜2.7 times between a pressure of 5 bars and 50 bars at 250° C.\|[0062] The preliminary results from the first reaction phase indicate that the kinetics of carbon dioxide mineralization increase with smaller grain sizes of the ore. There was a 23% improvement in the reduction of CO2 concentrations between 150 and 25 microns when holding temperature constant at 250° C., as determined based on CO2 pressure and concentration measurements and the mass of rock mineralized in the reaction vessel. While it is suspected that the removal of air will enhance the kinetics of carbon mineralization, at least one run without air/oxygen removal from the reactor vessel at the start of the first reaction phase did not appear to noticeably affect the carbonization reaction. Increasing both the temperature and the pressure of the reaction conditions increased the rate of CO2 mineralization up through at least 300° C. and 50 bars over reaction times of ˜18 hours in the batch experiments. Based on the plateau in the pressure of the reaction, these conditions are assumed to approach thermodynamic equilibrium in batch conditions between 12 and 18 hours, with variability observed throughout various experimental conditions (i.e., generally less time at higher temperature and pressure).\|[0063] During temperature increases from 100° C. to 300° C. at a constant pressure of 10 bars, the amount of mineralization increased from 14% additional mass (after 24 hours in a batch reactor) to 27%, representing a 92% increase in the mass of rock resulting from carbon mineralization. During pressure increases from 1 to 50 bar at a constant temperature of 250° C., the amount of mineralization increased from 4.1% additional mass (after 24 hours in a batch reactor) to 18.9%, representing a 4.6 times increase in the mass of rock resulting from carbon mineralization. Rotary kiln, fluidized bed, and toroidal bed processes were not evaluated in this process, but can be expected to substantially increase both the reaction rates and total efficiency of mineralization as compared to the batch process, even while temperature and pressure effects are expected to be similar to those in the batch process.\|[0064] In another experimental run, supercritical carbon dioxide was used in the reactor during the first reaction phase. Preliminary results indicate that the supercritical CO2 injected into the reactor at 10 bars and 250° C. reached a pressure plateau 4.5 hours (18.8%) faster than gaseous CO2. Thus, the carbon sequestration from this disclosed ex situ carbonation reaction may be maximized or enhanced while accounting for temperature and pressure in addition to other cost-intensive variables, such as energy input, material handling, and chemical processing costs. After the first reaction phase, the solid contents of the reactor were weighed. Based on a mass increase of between 39.3 grams (15.7%) at 150° C. at 5 bar and 101.6 grams (40.6%) at 300° C. at 50 bar, the abundance of total carbon mineralization was determined, which was verified using optical microscopy. Magnesite (i.e., magnesium carbonate), which was not observed in the initial experimental material, was identified, as expected based on the stoichiometry of the carbonation reaction resulting in a pre-concentration of an iron-rich iron-silica (fayalite and/or ferrosilite) phase prior to the second reaction phase.\|[0065] In the second reaction phase, liberation of the hydrogen was targeted through serpentinization/hydration reactions between the introduced water and the fayalite and/or ferrosilite (mixture in the four natural samples and exclusively olivine one prepared sample) in the remaining ore. Before the introduction of water with respect to the serpentinization reactions, the reactor vessel was evacuated using a mechanical rough pump to apply a vacuum and remove air from the reactor vessel including any remaining introduced carbon dioxide. Next, low oxygen fugacity (i.e., negative Eh value or negative electric potential), high pH (i.e., pH ranging between 8.3 and 11.1 using sodium bicarbonate or either sodium or potassium hydroxide), and saline (about 0.1 to 4.5 per mil sodium chloride (NaCl)) water, prepared as described above, was then introduced at room temperature and ambient atmospheric pressure into reactor vessel containing the remaining ore (i.e., unreacted ore consisting of the iron silicate phase, magnesium carbonate, silicon dioxide, residual olivine, pyroxene, and other accessory mineral phases).\|[0066] The initial gas phase pressure was measured/recorded via the sampling port using the standard Omega 0 to 100 psi pressure gauge. The temperature inside the reactor vessel was then increased to 50° C., 100° C., 150° C., 200° C., 250° C., 300° C., and 400° C. with the temperature being controlled by the external band heater and monitored with an Omega K-wire thermocouple. At each temperature step, the gas phase pressure was measured via the sampling port using the standard Omega 0 to 100 psi pressure gauge. At each temperature, an aliquot of gas was measured using a Stanford Research Systems residual gas analyzer (“quadrupole mass spectrometer”) and SRI gas chromatograph fitted with a thermocouple detector. The total pressure of hydrogen (and other gases) was calculated by determining the product of the percentage of hydrogen gas measured using the residual gas analyzer and/or gas chromatograph with the pressure compared to atmospheric pressure and assuming PV=nRT.\|[0067] The preliminary results from the second reaction phase indicated that the kinetics of hydrogen evolution increase with smaller grain sizes of the ore. There was a 5.2 times improvement in the yield of H2 between the temperature steps of 50° C. and 100° C. when holding a constant pressure of 10 bars as determined based on H2 partial pressure over a time interval of 18 hours. There was a 7.3 times improvement in the yield of H2 concentrations between the temperature steps of 100° C. and 400° C. when holding a constant pressure of 10 bars as determined based on H2 partial pressure over a time interval of 18 hours. The yield of H2 increased with pressure, but not to the same extent as temperature. There was a 31% times improvement in the yield of H2 between 1 and 5 bars at a constant temperature of 250° C., and a 1.8 times increase in the yield of H2 between 5 and 40 bars at a constant temperature of 250° C. as determined based on H2 partial pressure over a time interval of 18 hours. When compared to serpentinization reactions that were not preceded by the two-step carbonation reaction, the kinetic rates of the serpentinization reaction increase by 21% at 150° C. and up to 87% at 250° C. conducted at a constant pressure of 20 bars as compared to experiments performed at 100° C. This change is believed to be due to the carbonation-driven comminution of the ore that facilitated the initial breakdown of the rock/ore as well as the pre-concentration of the iron silicate mineral phases. The highest increase in the yield of H2 was 1.8 times above the yield observed at 100° C. and was observed at a temperature step of 200° C. following density separation of SiO2 and MgCO3 from the denser iron silicates by laboratory sluicing; this step yielded total H2 production of 0.576 mol H2/kg. Each increasing temperature step demonstrated an improvement in the purity of the hydrogen gas evolved; variable mixtures of N2, Ar and minor CO2 were observed in both the 50° C. and 100° C. temperature steps, which was less than 5% in the non-condensable fraction at temperatures above 150° C. with the exception of one sample at 400° C., which yielded 6.7% CO2.\|[0068] Along with the composition (%), the total pressure of the hydrogen gas that was formed by the reaction increased with higher temperatures, indicating a progressive increase in the kinetic rates and the total yield of hydrogen generation with higher temperature. Although this result was theoretically expected, it differentiates hydrogen produced by example embodiments described herein from hydrogen generated by natural systems wherein the occurrence of CO2, HCO3−, or other forms of carbon in the subsurface can begin to react with hydrogen at ˜150° C., which “short circuits” carbon-negative hydrogen generation by the formation of abiogenic methane via the Sabatier reaction (i.e., CO2+4H2→CH4+2H2O), wherein CO2 can be available as gaseous phase CO2 or be liberated from dissolved inorganic carbon phases in pore fluids by the following reaction: H++HCO3→CO2+H2O).\|[0069] A comparison of the disclosed two-step reaction was performed by further comparison to two base case single step reactions. The first base case comparison was a one-step reaction at a pH of 6.0 with temperatures increased from room temperature to 50° C., 100° C., 150° C., 200° C., 250° C., 300° C., and 400° C. The highest H2 yield at this pH was less than 0.011 mol H2/kg at 400° C., which was expected based on the mildly acidic conditions. The second base case comparison was a one-step reaction at a pH of 8.0 with temperatures increased from room temperature to 50° C., 100° C., 150° C., 200° C., 250° C., 300° C., and 400° C. At this pH and holding pressure constant at 20 bars, H2 yield in the single step reaction ranged from below detection limits at 50° C. at 18 hours to 0.051 mol H2/kg at 100° C. and up to 0.349 mol H2/kg at 400° C. For comparison, the highest value observed at the 400° C. in the single-step base case was 69.6% lower than the highest yield in the two-step reaction described above. Thus, the hydrogen gas production from this disclosed ex situ serpentinization reaction may be maximized or enhanced while accounting for temperature and pressure in addition to other cost-intensive variables, such as energy input, material handling, and chemical processing costs, especially by precluding interactions between H2 and labile carbon (i.e., CO2).\|[0070] After the sequential first and second reaction phases (i.e., the carbonation and serpentinization reactions) were completed in the reaction vessel, the mass (i.e., weight), mineralogy, and geochemical composition of the remaining bulk rock were determined by optical mineralogy and ICP-MS to evaluate the abundance (or lack) of relevant constituents (e.g., fayalite, ferrosilite, FeO, MgO, etc.). While visible olivine and pyroxene were still observed along with minor serpentine, the amount of magnetite observed was significantly higher (11-171% based on the mass of the separatable magnetic components) in the sequential reaction (i.e., first reaction phase followed by second reaction phase) than when the reaction was done without pre-concentration of the fayalite and/or ferrosilite minerals and control of reaction conditions, e.g., pH, low oxygen control, temperature. There was a 11% increase in the yield of magnetite between the temperature steps of 50° C. and 100° C. and approximately 13% between 100° C. and 150° C., while there was 1.7 times more magnetite recovered magnetically when comparing the 300° C. and 100° C. steps when holding a constant pressure of 10 bars over a time interval of 18 hours. Based on the stoichiometry of the reactions and these observations, it is apparent that an increased generation of magnetite is coupled with and inextricably linked to an increased generation of hydrogen (as was expected from the stoichiometric serpentinization reaction). These results support the stoichiometric modeling of both carbon dioxide mineralization (via carbonation) and hydrogen production (via serpentinization/hydration reactions). Thus, magnetite may be produced as a co-product of hydrogen generation/evolution (or vice versa based on the chosen business method).\|[0071] Additional analysis of the residual material identified highly elevated metal enrichments that included phosphates, aluminum oxides, and other poorly defined solids in the gangue (“mineral slag”). For example, lanthanum (one rare earth element) demonstrated an average concentration of 8.2 ppm in the bulk sample of ultramafic rock from the Pennsylvania quarry and 187.1 ppm in the residual gangue (largely aluminum oxide, phosphates and sulfides corresponding to roughly 2-4% of the total material). Similarly, nickel and cobalt concentrations were 133.9 and 78.2 ppm in a bulk sample of ultramafic rock from the same Pennsylvania quarry and 1,426 and 976.8 ppm in the residual gangue (largely aluminum oxide and sulfides). Separation of these metal enrichments may be accomplished by density separation techniques such as heavy liquid separation or other gravity separation, or sluicing or other methods known to those skilled in the art.\|[0072] The overall results indicate that, in the pursuit of carbon neutral or even negative carbon hydrogen production, the sequential carbonation and serpentinization reactions phases disclosed herein provide several reaction products (e.g., magnetite, rare earth elements, and other scarce metals) of economic and societal value in the pursuit of a lower carbon economy in addition to carbon sequestration and hydrogen evolution. Moreover, there exist a range of conditions where each reaction may be enhanced that varies only slightly with different rock contents, such that the reactions are more or less stable in the conditions described above among various sources of ultramafic and mafic rocks.\|[0073] As briefly discussed above, several reaction products have been identified from the staged, sequential carbonation and serpentinization reactions disclosed herein. Four reaction products in particular have the potential to be economically viable, especially when enhanced or enabled by steps, procedures, reaction conditions described herein that enhance the rock drivers comminution and thermodynamic toward idealized “carbonation” and serpentinization/hydration reactions. Adding to their economic viability, there may be revenue entitlements tied to the production of these reaction products, such as tax credits, sale of carbon credits, tax incentives, etc. The four products include: magnesite/aggregate, “green” or “golden” hydrogen (net carbon negative), magnetite, and scarce metals, and each will be discussed further hereinbelow.\|Magnesite\|[0074] The controlled ex situ generation of magnesite (magnesium carbonate) by enhancing “water-rock” serpentinization/hydration reactions involving mined, quarried, or waste (e.g., mine tailings) mafic or ultramafic rock and products provides an economic and carbon neutral (or even carbon negative) pathway for scalable magnesite and rock aggregate formation. This process can also economically increase the volume and mass of the rock (stoichiometric assessment of suitable mafic/ultramafic ores suggest the mass can increase by 34 to >60% (or 0.34 to >0.60 kg/kg of rock or 340 kg to >600 kg/metric ton of rock), while experimental results suggested at increase of 0.104 kg/kg (300° C. at 50 bars in the bulk rock obtained from the Pennsylvania quarry) to 0.237 kg/kg (300° C. at 50 bars in the pure olivine test sample). These values are expected to increase further by moving from a batch to dynamic reaction process (e.g., rotary kiln, fluidized bed, toroidal bed, or other similar processes) of rock compared to the original material introduced into the batch reactor.\|[0075] As disclosed, water having a pH of between about 4.8 to about 6.5 may be mixed with carbon dioxide in controlled conditions (e.g., under atmospheric or oxidizing conditions) to chemically break down the magnesium-rich silicate (i.e., forsterite) portion of mafic and ultramafic rocks. This reaction may be enhanced at temperatures of between about 150° C. to about 300° C. to 400° C. (although our experiment displayed a plateau in increased mineralization at 300° C.) and at pressures of at least up to 50 bars to produce magnesite. This carbonation process permanently sequesters carbon dioxide through the precipitation of magnesite mineral phases and other carbonate minerals, which can be used directly or as rock aggregate.\|[0076] The successful conversion of magnesium-silicate into magnesium carbonate and other carbonate minerals also allows the possibility to remove the bulk of the rock mass (following previously described density separation techniques) that can subsequently be either separated from residual iron-silicates or be separated prior to serpentinization/hydration reactions. The step of concentrating the iron silicate phase can further concentrate scarce metals (e.g., nickel, cobalt, rare earth elements) in other mineral forms (e.g., aluminum oxides, phosphates, and sulfides). This carbonation process is conducted first such that sequential serpentinization reactions may more readily and abundantly produce the reaction products of magnetite and hydrogen gas without the formation of accessory/competitive phases and enhance comminution.\|[0077] The importance of scalable and carbon negative (or carbon neutral) magnesium carbonate (magnesite) production has direct bearing on the numerous current uses of magnesite, including, but not limited to, pharmaceutical applications, agricultural lime and fertilizers (to neutralize acidification caused by fertilizer use), raw materials for ceramic and ceramic brick, and flux used in iron and steel manufacturing. Magnesite may also be used as a partial lime substitute to enable lower carbon emissions that result from the lower temperatures required to make magnesium oxide (MgO) as compared to calcium oxide (CaO). Further, magnesite can be used as a carbon negative concrete filler and cement or aggregate substitute in concrete.\|Green/Golden Hydrogen\|[0078] Hydration reactions involving iron-silicates (e.g., fayalite, ferrosilite) may be used to generate “green” (i.e., carbon neutral) or “golden” (i.e., carbon negative) hydrogen ex situ from mined, quarried, or waste streams of olivine- and/or pyroxene-rich ores, such as mafic and ultramafic rock. In one or more embodiments of the systems and method disclosed herein, the ex situ generation of carbon-negative hydrogen is directed to a two-reaction step/phase process in which: (1) carbon dioxide is first introduced in a gaseous or supercritical state into pulverized rock (approximately <150 microns) that has been wetted with a water preparation having a pH of between about 4.8 and about 6; and (2) water with a low oxygen fugacity (e.g., obtained from municipal wastewater, geothermal water, or other industrial water uses or made by reacting tap water over a bed of copper at 125° C.), a pH of between 8.3 and about 11.1 (the specified pH attained by adding sodium bicarbonate or either sodium or potassium hydroxide to the water but such water pH may be found in natural sources of water and wastewater) across a temperature range of between about 60° C. and about 400° C.\|[0079] The removal of a substantial portion of magnesium component from the powdered or comminuted rock in the first reaction phase increases the chemical (reaction) potential of the iron-rich portion in the second reaction phase. Stoichiometric calculations suggest that the chemical activity can be increased by up to eight times, while improvements of approaching a factor of two were observed in experiments; it is anticipated that the chemical activity and kinetics can be further increased by transitioning from a batch to dynamic process. Indeed, the rates of hydrogen production are significantly greater (nearly 70% greater) than in a method in which the iron-rich silicate mineral is reacted without the precursor step of carbon dioxide mineralization compared to a suitable base case for natural reactions or other one step engineered reaction processes.\|[0080] A significant advantage of various embodiments disclosed herein is that the systems and methods of such embodiments can be set up for ex situ operation almost anywhere in the world due to the vast and far-reaching reserves of mafic and ultramafic rock and availability of water and chemicals for amendment of pH and Eh of the water. Conversely, hydrogen formation in a more conventional manner, such as by natural gas reforming, is limited by natural gas availability, among other constraints that are often carbon intensive. Even if the produced carbon dioxide is sequestered, the hydrogen would be considered “blue,” not “green” or “golden.”\|Magnetite\|[0081] The controlled ex situ generation of magnetite by enhancing “water-rock serpentinization” reactions on mined, quarried, or waste streams of olivine- and/or pyroxene-rich ores and other materials provides an economic and carbon neutral (or even carbon negative) pathway for the production of magnetite while also enabling commensurate carbon dioxide sequestration through carbonate mineralization. While carbonation and serpentinization reactions are themselves naturally occurring, embodiments of the systems and methods disclosed herein are directed to enhanced magnetite production through the sequential ordering of these reactions in a controlled ex situ environment to limit alternative and undesirable chemical reactions capable of producing serpentine, brucite, or asbestos.\|[0082] In various embodiments disclosed herein, the ex situ generation of magnetite is directed to a two-reaction step/phase process in which: (1) carbon dioxide is first introduced in a gaseous or supercritical state in the presence of pulverized rock (approximately <150 microns) that has been wetted with a water preparation having a pH of between about 4.8 and about 6.5; and (2) water with a low oxygen fugacity (e.g., obtained from municipal wastewater, geothermal water, treated groundwater or other industrial water uses or made by reacting tap water over a bed of copper at 125° C.) having a pH of between 8.3 and about 11.1 (the specified pH attained by adding sodium bicarbonate or either sodium or potassium hydroxide to the water but such water pH may be found in natural sources of water and wastewater) is introduced across a temperature range of between about 80° C. and about 400° C. The two-step reaction at temperature >300° C. improves magnetite recovery by ˜1.7 times compared to lower temperatures and a suitable base case. Further, removal of a substantial portion of magnesium component from the powdered or comminuted rock in the first reaction step/phase increases the chemical (reaction) potential of the iron-rich portion in the second reaction step/phase (e.g., by approximately 23-800%), thereby increasing the thermodynamic drivers of magnetite generation several times. Thus, the generation of preferred mineral products, such as magnetite and hydrogen, is increased when compared to the random or undesired mineral species typically generated in natural systems. Indeed, the rates of magnetite production are significantly greater, and the targeted production of these specific chemical species is more reliable (e.g., the formation of serpentine, brucite, or asbestos are reduced) than in a method in which the iron-rich silicate mineral is reacted without the precursor step of carbon dioxide mineralization or in which both CO2 and water are reacted together (which occurs in natural systems).\|[0083] The Direct Reduction Iron (DRI) process is the only commercial low carbon emissions iron making process, and it is a precursor to steel manufacturing. The DRI process requires high-grade iron ore (greater than approximately 67% iron), which is in short supply in natural iron ores worldwide. Such limited access to magnetite (or other similarly iron-rich mineral phases) limits the potential to produce iron or steel using the DRI process, which is an important pathway for reducing carbon dioxide emissions in the steel industry. The systems and methods disclosed herein may produce high-grade iron ore (magnetite) in vast quantities due to the prolific occurrence of mafic and ultramafic rock, which accounts for greater than 10% of the continental crust and the vast majority of the oceanic crust. Moreover, the carbon dioxide sequestration tax credits and/or carbon credit sales associated with magnesite production may be attached to the magnetite output of these systems and methods. Thus, embodiments disclosed herein may increase the availability of high-grade iron ore to the steel industry along with a carbon credit, which may also result in the “greening” of the steel industry worldwide. Notably, the collective co-production (at one physical site) of magnesite, magnetite, and hydrogen gas also satisfies three requirements (i.e., iron-rich iron ore; reductive gas species/hydrogen; and magnesite flux) of iron making processes.\|Scarce Metals\|[0084] Elevated concentrations of certain relatively scarce metals (e.g., nickel, cobalt, chromium, and rare earth elements) in mafic and ultramafic rocks may be liberated and more easily recovered ex situ through sequential carbon sequestration/carbonation and “water-rock” serpentinization reactions involving mined, quarried, or waste mafic or ultramafic rock/ore. These scarce, and in some cases strategic, metals are critical for renewable energy and energy storage and are often derived from mining of weathered or processed minerals in more energy intensive steps (i.e., dehydration of asbestos back to forsterite). However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide. The reaction of gaseous or supercritical carbon dioxide with forsterite chemically breaks down these magnesium-rich silicate minerals and simultaneously sequesters carbon from carbon dioxide, while the reaction of water with fayalite and/or ferrosilite chemically breaks down the iron-rich silicate minerals and simultaneously produces magnetite and hydrogen gas. With the breakdown of these minerals, the remaining scarce metals are concentrated in the remaining unreacted ore and gangue (i.e., aluminosilicates, phosphates, accessory oxides, clay, etc.). Thus, the kinetic rates of the reactions of one or more embodiments disclosed herein and total metal recovery (i.e., higher concentrations in the starting composition) are much increased over natural chemical weathering of mafic and ultramafic rock. Further, the concentration of scarce metals is increased in the gangue, and the carbon footprint of “mining” or recovering these precious metals (and their derivative utilization in mobility and energy storage) is reduced. Therefore, the sequential carbonation and serpentinization reactions may provide for what is, in essence, a carbon negative mining of scarce and strategic metals.\|Conclusion\|[0085] Many modifications and other embodiments of the inventions set forth herein will come to mind to one skilled in the art to which these inventions pertain having the benefit of the teachings presented in the foregoing descriptions and the associated drawings. Therefore, it is to be understood that the inventions are not to be limited to the specific embodiments disclosed and that modifications and other embodiments are intended to be included within the scope of the appended claims. Moreover, although the foregoing descriptions and the associated drawings describe example embodiments in the context of certain example combinations of elements and/or functions, it should be appreciated that different combinations of elements and/or functions may be provided by alternative embodiments without departing from the scope of the appended claims. In this regard, for example, different combinations of elements and/or functions than those explicitly described above are also contemplated as may be set forth in some of the appended claims. Although specific terms are employed herein, they are used in a generic and descriptive sense only and not for purposes of limitation.	Family Number\|(104224295)\|104224295\|Object of Invention\|(WO202307466 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US20230102312 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US20230271827 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US12006212 B2)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(CA3227505 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(AU2022318480 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(IN202417013808 A)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US20240308843 A1)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|(US12545576 B2)\|However, the disclosed system and method provides an economic and carbon neutral (or even carbon negative) pathway for the production of these scarce metals, while also enabling carbon sequestration by mineralization of carbon dioxide.\|Advantages / Prev. Drawbacks\|(JP2024528907 A)\|The remaining rocks are advantageously deposited for the following section reaction steps by both of the grinding of the raw rock and the carbonation reaction occurring during the first reaction step, so that various combinations of grinding and the first reaction step can be used in various scenarios based on the desired result of a predetermined embodiment.\|	Environmental technology\|Materials, 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JP202020032422; US4798717; US20040087178; US20080299024; US20090308731; US20100313794; US20150152784; US20150157979; US20190131645; EP-236480; JP2020032422; JP2021513460; WO2013100333; WO2017222396; WO2019153047; WO2021138653; WO2023239797\|US20100313794; US20080299024; US20040087178; US20190131645; US4798717; US20190031645; US20150152784; US20090308731; US20150157979; WO2013100333; WO2021138653\|XP085850195; US20150157979; XP093030447; US20090308731; WO2013100333; WO2021138653\|\|US20150157979; US20090308731; WO2013100333; WO2021138653; XP085413764; WO2023239797; EP-236480; XP036373985\|US20150157979; JP2021513460; WO2017222396; JP2020032422\|\|\|\|	(EP4377258)\|Search Report references [Examiner]\|-KULARATNE KANCHANA ET AL: "Simultaneous ex-situ CO2mineral sequestration and hydrogen production from olivine-bearing mine tailings", APPLIED GEOCHEMISTRY, PERGAMON, AMSTERDAM, NL, vol. 95, 30 May 2018 (2018-05-30), pages 195 - 205, XP085413764, ISSN: 0883-2927, DOI: 10.1016/J.APGEOCHEM.2018.05.020\|-BASSEZ MARIE-PAULE ED - PIZZARELLO SANDRA: "Anoxic and Oxic Oxidation of Rocks Containing Fe(II)Mg-Silicates and Fe(II)-Monosulfides as Source of Fe(III)-Minerals and Hydrogen. Geobiotropy", ORIGINS OF LIFE AND EVOLUTION OF THE BIOSPHERE, KLUWER ACADEMIC PUBLISHERS, DORDRECHT, NL, vol. 47, no. 4, 31 March 2017 (2017-03-31), pages 453 - 480, XP036373985, ISSN: 0169-6149, [retrieved on 20170331], DOI: 10.1007/S11084-017-9534-5\|-See also references of WO 2023007466A1\|\|(US12545576)\|Examiner references\|-Kularatne et al. “Simultaneous ex-situ CO2 mineral sequestration and hydrogen production from olivine-bearing mine tailings.” Applied Geochemistry 95, p. 195-218 (2018).\|-Ehlmann, et al., “Ambient and cold-temperature infrared spectra and IRD patterns of ammoniated phyllosilcates and carbonaceous chondrite meteorites relevant to Ceres and other solar system bodies,” Meteorites Planetary Science, vol. 53, No. 9 (2018).\|-Wang, et al., “Pyroxene control H2 production and carbon storage during water-periodotite-CO2 hydrothermal reactions,” International Journal of Hydrogen Energy, vol. 44, p. 26835-26847; Sep. 11, 2019.\|-Bassez, Marie-Paule, “Anoxic and Oxic Oxidation of Rocks Containing Fe(II)Mg-Silicates and Fe(II)-Monosulfides as Source of Fe(III)-Minerals and Hydrogen. Geobiotropy”, Origins of Life and Evolution of the Biosphere, Kluwer Academic Publishers, vol. 47, No. 4, Mar. 31, 2017 (Mar. 31, 2017), pp. 453-480.\|\|(US12006212)\|Search Report references [Examiner]\|-Kularatne et al. "Simultaneous ex-situ CO2 mineral sequestration and hydrogen production from olivine-bearing mine tailings." APplied Geochemistry 95 (2018) 195-218 (Year: 2018)\|-Kularatne et al. “Simultaneous ex-situ CO2 mineral sequestration and hydrogen production from olivine-bearing mine tailings.” Applied Geochemistry 95 (2018) 195-218 (Year: 2018).\|-Ehlmann, et al., Ambient and cold-temperature infrared spectra and IRD patterns of ammoniated phyllosilcates and carbonaceous chondrite meteorites relevant to Ceres and other solar system bodies, Meteorites & Planetary Science, vol. 53, No. 9, 2018 [retrieved on Oct. 5, 2022]. Retrieved from the internet, <URL:https://onlinelibrary.wiley.com/dol/pdf/10.1111/maps.13103>, pp. 1884-1901.\|-Wang, et al., Pyroxene control H2 production and carbon storage during water-peridotite-CO2 hydrothermal reactions, International Journal of Hydrogen Energy, vol. 44, Sep. 11, 2019, pp. 26835-26847.\|\|\|(WO2023/007466)\|International Search Report [Examiner]\|-WANG ET AL.: "Pyroxene control of H2 production and carbon storage during water-peridotite-CO2 hydrothermal reactions", INTERNATIONAL JOURNAL OF HYDROGEN ENERGY, vol. 44, 11 September 2019 (2019-09-11), pages 26835 - 26847, XP085850195, DOI: 10.1016/j.ijhydene.2019.08.161\|-EHLMANN BETHANY L., ROBERT HODYSS, THOMAS F. BRISTOW, GEORGE R. ROSSMAN, ELEONORA AMMANNITO, M. CRISTINA DE SANCTIS, CAROL A. RAYM: "Ambient and cold-temperature infrared spectra and XRD patterns of ammoniated phyllosilicates and carbonaceous chondrite meteorites relevant to Ceres and other solar system bodies", METEORITICS & PLANETARY SCIENCE, vol. 53, no. 9, 23 April 2018 (2018-04-23), pages 1884 - 1901, XP093030447, DOI: 10.1111/maps.13103\|-See also references of EP 4377258A4\|\|\|\|\|\|	GRANTED	(EP4377258)\|PENDING\|(US12545576)\|GRANTED\|(US12006212)\|GRANTED\|(US20230102312)\|LAPSED\|(WO2023/007466)\|LAPSED\|(JP2024528907)\|REVOKED\|(BR112024001825)\|PENDING\|(IN202417013808)\|PENDING\|(AU2022318480)\|PENDING\|(CA3227505)\|PENDING	ALIVE	(EP4377258)\|ALIVE\|(US12545576)\|ALIVE\|(US12006212)\|ALIVE\|(US20230102312)\|DEAD\|(WO2023/007466)\|DEAD\|(JP2024528907)\|DEAD\|(BR112024001825)\|ALIVE\|(IN202417013808)\|ALIVE\|(AU2022318480)\|ALIVE\|(CA3227505)\|ALIVE	(EP4377258)\|LEGAL DETAILS FOR EP4377258\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-07-29\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP22848809\|Application date=2022-07-29\|Standardized application number=2022EP-0848809\|Event publication date=2023-02-03\|Event code=EP/STAAPCT\|Event group=Examination events Entry into national phase\|The international publication has been made\|Original code: STAA\|Event publication date=2024-05-03\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2024-05-03\|Event code=EP/STAARQ\|Event indicator=Pos\|Event group=Examination events\|Request for examination was made\|Original code: STAA\|Event publication date=2024-06-05\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP4377258\|Publication stage code=A1\|Publication date=2024-06-05\|Standardized publication number=EP4377258\|Event publication date=2024-06-05\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2024-02-20\|Event publication date=2024-06-05\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2024-11-06\|Event code=EP/DAV\|Event indicator=Neg\|Event group=Designated states\|Request for validation of the European patent (deleted)\|Request for validation of the european patent (in any country) deleted\|Event publication date=2024-11-06\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2025-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Examination events\|Supplementary search report\|Ergaenzender recherchenbericht\|Publication country=EP\|Publication number=EP4377258\|Publication stage code=A4\|Publication date=2025-09-17\|Standardized publication number=EP4377258\|Event publication date=2025-09-17\|Event code=EP/A4\|Event indicator=Pos\|Event group=Administrative notifications\|Supplementary search report drawn up and despatched\|Effective date of the event=2025-08-19\|Event publication date=2025-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication date=2025-09-17\|Event code=EP/RIC1\|Event group=Classification modifications Corrections\|Information provided on IPC code assigned before grant\|Event publication 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code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1735\|Event publication date=2023-04-18\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 2890822.00005\|Event publication date=2023-04-18\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 178846\|Event publication date=2023-04-18\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2023-04-18\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2023-04-18\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2023-04-18\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2023-04-18\|Event code=US/ENT\|Event group=Administrative 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OAO\|Restriction/Election Requirement\|Event publication date=2023-08-31\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20230271827\|Publication stage code=A1\|Publication date=2023-08-31\|Standardized publication number=US20230271827\|Event publication date=2023-08-31\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2023-09-12\|Event code=US/ELC\|Event group=Examination events OAI\|Response to Election / Restriction Filed\|Event publication date=2023-10-07\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2023-10-12\|Event code=US/112NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 112 - subject matter in claims not properly defined\|RJD=2023-10-12\|R4R=112b\|RJST=non-final\|Rejected claims 17\|Event publication date=2023-10-12\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2023-10-12\|R4R=102a\|RJST=non-final\|Rejected claims 8, 13, 14\|RJCT=US20100313794\|Event publication date=2023-10-12\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2023-10-12\|R4R=103\|RJST=non-final\|Rejected claims 1, 8, 13-15; 2, 3; 4; 5, 11; 7, 9-10, 16; 9-10, 16; 17\|RJCT=US20080299024\|RJCT=US20040087178\|RJCT=US20190131645\|RJCT=US20100313794\|RJCT=US4798717\|RJCT=US20190031645\|Event publication date=2024-01-12\|Event code=US/INVSUM\|Event group=Examination events OAI INT\|Interview Summary- Applicant Initiated\|Event publication date=2024-01-16\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2024-02-05\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2024-02-07\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2024-05-07\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DARRAH, THOMAS;RAO, VIKRAM;WHYTE, COLIN\|Reel/frame:067334/0570\|OWNER:OHIO STATE INNOVATION FOUNDATION, OHIO\|Effective date of the event=2021-07-30\|Event publication date=2024-05-07\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2024-05-07\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2024-05-09\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2024-05-22\|Event code=US/PAT\|Event indicator=Pos\|Event group=Event indicating In Force\|Patented Case\|Event publication date=2024-05-22\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2024-06-11\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US12006212\|Publication stage code=B2\|Publication date=2024-06-11\|Standardized publication number=US12006212\|Event publication date=2024-06-11\|Event code=US/MEPGNTF\|Event group=Event indicating In Force Administrative notifications\|Mail Patent eGrant Notification\|Event publication date=2024-06-11\|Event code=US/EPGNTF\|Event group=Event indicating In Force Administrative notifications\|Patent eGrant Notification\|Event publication date=2024-06-11\|Event code=US/EPG\|Event group=Event indicating In Force\|Recordation of Patent eGrant\|Event publication date=2024-06-11\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 0 Adjustment total: \|Number of days of extension=0\|(US20230102312)\|LEGAL DETAILS FOR US20230102312\|Actual or expected expiration date=2023-06-09\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-07-28\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US17815914\|Application date=2022-07-28\|Standardized application number=2022US-17815914\|Event publication date=2022-07-28\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:HOUSE, KIMBERLY ANN\|Event publication date=2022-07-28\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 178846\|Event publication date=2022-07-28\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=Yes\|Event publication date=2022-07-28\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=3974\|Event publication date=2022-07-28\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 2890822.00002\|Event publication date=2022-07-28\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Business Entity Status: Small\|Event publication date=2022-07-28\|Event code=US/PET\|Event group=APL\|Petition Entered\|Event publication date=2022-07-28\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2022-07-28\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:DARRAH, THOMAS;RAO, VIKRAM;WHYTE, COLIN\|Reel/frame:060664/0083\|OWNER:OHIO STATE INNOVATION FOUNDATION, OHIO\|Effective date of the event=2021-07-30\|Event publication date=2022-08-08\|Event code=US/SMALL\|Event group=Administrative notifications\|Appl Has Filed a Verified Statement of Micro to Small Entity Status\|Event publication date=2022-08-10\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2022-12-09\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2022-12-09\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2022-12-23\|Event code=US/PTDI\|Event group=OAO\|Petition Decision - Dismissed\|Event publication date=2022-12-23\|Event code=US/RECEIPTUP\|Event group=Administrative notifications OAO\|Filing Receipt - Updated\|Event publication date=2023-01-09\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-01-30\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2023-03-30\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20230102312\|Publication stage code=A1\|Publication date=2023-03-30\|Standardized publication number=US20230102312\|Event publication date=2023-03-30\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2023-06-09\|Event code=US/ABNEA\|Event indicator=Neg\|Event group=Event indicating Not In Force OAI\|Expressly Abandoned -- During Examination\|Event publication date=2023-06-09\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2023-06-09\|Event code=US/ODPD6\|Event group=Administrative notifications\|GRANTED - Express Abandonment Petition Decision under 37 CFR 1.138 (d)\|(WO2023/007466)\|LEGAL DETAILS FOR WO2023/007466\|Actual or expected expiration date=2025-01-30\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2022-07-29\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOIB2022/057088\|Application date=2022-07-29\|Standardized application number=2022WO-IB57088\|Event publication date=2023-02-02\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2023/007466\|Publication stage code=A1\|Publication date=2023-02-02\|Standardized publication number=WO202307466\|Event publication date=2025-01-30\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2022318480\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2022318480\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2022AU-0318480\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2022318480\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2024-02-22\|Publication number in the designated or member state=AU2022318480\|Event publication date=2024-02-07\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=AU\|Event publication date=2024-02-22\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=AU\|MEMBER STATE LEGAL DETAILS FOR BR112024001825\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=BR Corresponding appl: BR112024001825\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2024BR-0001825\|Corresponding cc:\|Designated or member state=BR Corresponding pat: BR112024001825\|Publication stage code in the designated or member state=A0\|Publication date in the designated or member state=2024-02-06\|Publication number in the designated or member state=BR112024001825\|Event publication date=2024-02-06\|Event code=WO/REG\|Event code=BR/B01A\|Event group=Examination events\|Reference to a national code\|Pct publication - request for entry into the national phase\|Comunicacao da publicacao internacional pct. apresentacao de peticao de requerimento de entrada na fase nacional\|Corresponding cc:\|Designated or member state=BR\|Event publication date=2024-04-24\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2024-01-29\|Corresponding cc:\|Designated or member state=BR\|MEMBER STATE LEGAL DETAILS FOR CA3227505\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=CA Corresponding appl: CA3227505\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2022CA-3227505\|Corresponding cc:\|Designated or member state=CA Corresponding pat: CA3227505\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2023-02-02\|Publication number in the designated or member state=CA3227505\|Event publication date=2024-01-30\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=CA\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2024-03-01\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2024-03-01\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP4377258\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP22848809\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2022EP-0848809\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP4377258\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2024-06-05\|Publication number in the designated or member state=EP4377258\|Event publication date=2023-03-15\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2024-02-29\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2024-03-03\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Effective date of the event=2024-02-29\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR IN202417013808\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Corresponding cc:\|Designated or member state=IN Corresponding appl: IN202417013808\|Application date in the designated or member state=2024-02-26\|Application number in the designated or member state=2024IN-17013808\|Corresponding cc:\|Designated or member state=IN Corresponding pat: IN202417013808\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2024-03-15\|Publication number in the designated or member state=IN202417013808\|Event publication date=2024-02-26\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=IN\|MEMBER STATE LEGAL DETAILS FOR JP2024528907\|Actual or expected expiration date=2026-03-09\|Legal state=DEAD\|Status=REVOKED\|Corresponding cc:\|Designated or member state=JP Corresponding appl: JP2024505303\|Application date in the designated or member state=2022-07-29\|Application number in the designated or member state=2024JP-0505303\|Corresponding cc:\|Designated or member state=JP Corresponding pat: JP2024528907\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2024-08-01\|Publication number in the designated or member state=JP2024528907\|Event publication date=2024-01-29\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national phase\|Corresponding cc:\|Designated or member state=JP\|(JP2024528907)\|LEGAL DETAILS FOR JP2024528907\|Actual or expected expiration date=2026-03-09\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2022-07-29\|Event code=JP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=JP JP2024505303\|Application date=2022-07-29\|Standardized application number=2024JP-0505303\|Event publication date=2024-05-21\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2024-03-22\|Event publication date=2024-05-21\|Event code=JP/A621\|Event indicator=Pos\|Event group=Examination events\|Written request for application examination\|Japanese intermediate code: A621\|Effective date of the event=2024-03-22\|Event publication date=2024-08-01\|Event code=JP/A\|Event group=Examination events\|Published application\|Publication country=JP\|Publication number=JP2024528907\|Publication stage code=A\|Publication date=2024-08-01\|Standardized publication number=JP2024528907\|Event publication date=2025-03-19\|Event code=JP/A977\|Event group=Examination events\|Report on retrieval\|Japanese intermediate code: A971007\|Effective date of the event=2025-03-19\|Event publication date=2025-04-15\|Event code=JP/A131\|Event indicator=Neg\|Event group=Examination events\|Notification of reasons for refusal\|Japanese intermediate code: A131\|Effective date of the event=2025-04-15\|Event publication date=2025-07-14\|Event code=JP/A601\|Event group=Examination events\|Written request for extension of term\|Japanese intermediate code: A601\|Effective date of the event=2025-07-14\|Event publication date=2025-08-04\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2025-08-04\|Event publication date=2025-08-19\|Event code=JP/A131\|Event indicator=Neg\|Event group=Examination events\|Notification of reasons for refusal\|Japanese intermediate code: A131\|Effective date of the event=2025-08-19\|Event publication date=2025-11-18\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2025-11-18\|Event publication date=2025-12-09\|Event code=JP/A02\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Decision of refusal\|Japanese intermediate code: A02\|Effective date of the event=2025-12-09\|Event publication date=2025-12-09\|Event code=JP/RF121\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Article 121 of the Patent Act, Expected Rejection Date\|Effective date of the event=2026-03-09\|Event publication date=2026-04-08\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2026-04-08\|(BR112024001825)\|LEGAL DETAILS FOR BR112024001825\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-07-29\|Event code=BR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=BR BR112024001825\|Application date=2022-07-29\|Standardized application number=2024BR-0001825\|Event publication date=2024-02-06\|Event code=BR/A0\|Event indicator=Pos\|Event group=Examination events\|Application filed, as announced in the Gazette published by this office\|Publication country=BR\|Publication number=BR112024001825\|Publication stage code=A0\|Publication date=2024-02-06\|Standardized publication number=BR112024001825\|Event publication date=2024-04-24\|Event code=BR/A2\|Event indicator=Pos\|Event group=Examination events\|Application for a patent of invention / pipeline patent published without search report\|Publication country=BR\|Publication number=BR112024001825\|Publication stage code=A2\|Publication date=2024-04-24\|Standardized publication number=BR112024001825\|(IN202417013808)\|LEGAL DETAILS FOR IN202417013808\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2024-02-26\|Event code=IN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=IN IN202417013808\|Application date=2024-02-26\|Standardized application number=2024IN-17013808\|Event publication date=2024-03-15\|Event code=IN/A\|Event indicator=Pos\|Event group=Examination events\|Application laid open\|Publication country=IN\|Publication number=IN202417013808\|Publication stage code=A\|Publication date=2024-03-15\|Standardized publication number=IN202417013808\|(AU2022318480)\|LEGAL DETAILS FOR AU2022318480\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-07-29\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2022318480\|Application date=2022-07-29\|Standardized application number=2022AU-0318480\|Event publication date=2024-02-22\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2022318480\|Publication stage code=A1\|Publication date=2024-02-22\|Standardized publication number=AU2022318480\|(CA3227505)\|LEGAL DETAILS FOR CA3227505\|Actual or expected expiration date=2042-07-29\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2022-07-29\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA3227505\|Application date=2022-07-29\|Standardized application number=2022CA-3227505\|Event publication date=2023-02-02\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA3227505\|Publication stage code=A1\|Publication date=2023-02-02\|Standardized publication number=CA3227505\|Event publication date=2024-02-02\|Event code=CA/EEER\|Event indicator=Pos\|Event group=Examination events\|Examination request\|Effective date of the event=2024-01-30\|Event publication date=2024-07-19\|Event code=CA/MFA\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|MAINTENANCE FEE FOR APPLICATION PAID\|Annual fees payment date=2024-07-19\|Year of payment of annual fees=2\|Fee description text: MF (APPLICATION, 2ND ANNIV.) - SMALL\|Event publication date=2024-07-19\|Event code=CA/U00\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FEE PAID\|ST27 STATUS EVENT CODE: A-2-2-U10-U00-U101 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE REQUEST RECEIVED\|Effective date of the event=2024-07-19\|Event publication date=2024-07-19\|Event code=CA/U11\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FULL RENEWAL OR MAINTENANCE FEE PAID\|ST27 STATUS EVENT CODE: A-2-2-U10-U11-U102 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE FEE PAYMENT PAID IN FULL\|Effective date of the event=2024-07-19\|Event publication date=2025-07-25\|Event code=CA/MFA\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|MAINTENANCE FEE FOR APPLICATION PAID\|Annual fees payment date=2025-07-25\|Year of payment of annual fees=3\|Fee description text: MF (APPLICATION, 3RD ANNIV.) - SMALL\|Event publication date=2025-07-25\|Event code=CA/U00\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FEE PAID\|ST27 STATUS EVENT CODE: A-2-2-U10-U00-U101 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE REQUEST RECEIVED\|Effective date of the event=2025-07-25\|Event publication date=2025-07-25\|Event code=CA/U11\|Event indicator=Pos\|Event group=Payment or non-payment notifications\|FULL RENEWAL OR MAINTENANCE FEE PAID\|ST27 STATUS EVENT CODE: A-2-2-U10-U11-U102 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: MAINTENANCE FEE PAYMENT PAID IN FULL\|Effective date of the event=2025-07-25\|Event publication date=2025-10-27\|Event code=CA/D15\|Event group=Examination events\|EXAMINATION REPORT COMPLETED\|ST27 STATUS EVENT CODE: A-2-2-D10-D15-D126 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: EXAMINER'S REPORT\|Effective date of the event=2025-10-27\|Event publication date=2026-02-25\|Event code=CA/P11\|Event group=Corrections Examination events\|AMENDMENT OF APPLICATION REQUESTED\|ST27 STATUS EVENT CODE: A-2-2-P10-P11-P100 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: AMENDMENT RECEIVED - RESPONSE TO EXAMINER'S REQUISITION\|Effective date of the event=2026-02-25\|Event publication date=2026-02-26\|Event code=CA/P11\|Event group=Corrections Examination events\|AMENDMENT OF APPLICATION REQUESTED\|ST27 STATUS EVENT CODE: A-2-2-P10-P11-P102 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: AMENDMENT DETERMINED COMPLIANT\|Effective date of the event=2026-02-26\|Event publication date=2026-02-26\|Event code=CA/P13\|Event group=Corrections\|APPLICATION AMENDED\|ST27 STATUS EVENT CODE: A-2-2-P10-P13-X000 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: APPLICATION AMENDED\|Effective date of the event=2026-02-26\|Event publication date=2026-02-26\|Event code=CA/W00\|Event group=Administrative notifications\|OTHER EVENT OCCURRED\|ST27 STATUS EVENT CODE: A-2-2-W10-W00-W111 (AS PROVIDED BY THE NATIONAL OFFICE)\|Event text: CORRESPONDENT DETERMINED COMPLIANT\|Effective date of the event=2026-02-26	(EP4377258)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(WO2023/007466)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2023/007466)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2023/007466)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2023/007466)\|OAPI: ST, KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2023/007466)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IQ, IR, IS, AL, IT, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, JM, RU, BG, JO, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, KG, KH, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, KW, CR, KZ, CU, CV, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, DJ, LR, TZ, DK, LS, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, WS, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(EP4377258)\|EP; DE\|(US12545576)\|US\|(US12006212)\|US\|(WO2023/007466)\|AU; BR; CA; EP; IN\|(BR112024001825)\|BR\|(IN202417013808)\|IN\|(AU2022318480)\|AU\|(CA3227505)\|CA	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=8TP/cX+h8x4s9VnBCZbBPnmXtI+wKb3KNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US0000000023293142&ekey=1944&xpn=EP4377258&kind=A4	https://register.epo.org/application?number=EP22848809	https://permalink.orbit.com/RenderStaticFirstPage?XPN=aIV65hZo%252BWIbWDK85JFymXfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	US	(US12545576)\|US\|(US20240308843)\|US\|(US12006212)\|US\|(US20230271827)\|US\|(WO2023/007466)\|US\|(US20230102312)\|US	(US12545576)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US , ATYP=US State Government\|(US20240308843)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US\|(US12006212)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US , ATYP=US Company\|(US20230271827)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US\|(WO2023/007466)\|NAME=OHIO STATE INNOVATION FOUNDATION 1524 North High Street Columbus, Ohio 43201 , COUNTRY=US\|(US20230102312)\|NAME=Ohio State Innovation Foundation , CITY=Columbus , STATE=OH , COUNTRY=US	(EP4377258)\|DE\|\|\|(WO2023/007466)\|US\|\|(AU2022318480)\|AU\|(CA3227505)\|CA	(EP4377258)\|NAME=K&L Gates LLP;Karolinen Karree Karlstraße 12 , CITY=80333 München , COUNTRY=DE , REG=101744768\|(US12545576)\|NAME=K&L Gates LLP\|(US12006212)\|NAME=K&L Gates LLP\|(WO2023/007466)\|NAME=EASWARAN, David Womble Bond Dickinson (US) LLP Attn: Patent Docketing P.O. Box 570489 Atlanta, Georgia 30357 , POSTCODE=30357 , COUNTRY=US\|(JP2024528907)\|NAME=KIMURA, Mitsuru , REG=100095407NAME=Yasushi Morikawa , REG=100132883NAME=Kei Sakurada , REG=100148633NAME=Hide Mie , REG=100147924\|(AU2022318480)\|NAME=K&L Gates Level 25 South Tower 525 Collins Street , CITY=Melbourne , STATE=VIC , POSTCODE=3000 , COUNTRY=AU\|(CA3227505)\|NAME=ROWAND LLP , COUNTRY=CA	\|(EP4377258)\|US; US; US\|(US12545576)\|US; US; US\|(US20240308843)\|US; US; US\|(US12006212)\|US; US; US\|(US20230271827)\|US; US; US\|(US20230102312)\|US; US; US\|(WO2023/007466)\|US; US; US\|\|\|\|\|(CA3227505)\|US; US; US	(EP4377258)\|NAME=DARRAH, Thomas\|NAME=RAO, Vikram\|NAME=WHYTE, Colin\|(EP4377258)\|NAME=DARRAH, Thomas, CITY=Columbus, Ohio 43210, COUNTRY=US \|NAME=RAO, Vikram, CITY=Columbus, Ohio 43210, COUNTRY=US \|NAME=WHYTE, Colin, CITY=Columbus, Ohio 43210, COUNTRY=US\|(US12545576)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(US20240308843)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(US12006212)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(US20230271827)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(US20230102312)\|NAME=Darrah Thomas, CITY=Westerville, STATE=OH , COUNTRY=US \|NAME=Rao Vikram, CITY=Chapel Hill, STATE=NC , COUNTRY=US \|NAME=Whyte Colin, CITY=Grove City, STATE=OH , COUNTRY=US\|(WO2023/007466)\|NAME=DARRAH, Thomas c/o 1524 North High Street Columbus, Ohio 43210, POSTCODE=43210, COUNTRY=US \|NAME=RAO, Vikram c/o 1524 North High Street Columbus, Ohio 43210, POSTCODE=43210, COUNTRY=US \|NAME=WHYTE, Colin c/o 1524 North High Street Columbus, Ohio 43210, POSTCODE=43210, COUNTRY=US\|(JP2024528907)\|NAME=THOMAS DARRAH\|NAME=Rao, Bikram\|NAME=COLIN WHYTE\|(BR112024001825)\|NAME=DARRAH THOMAS\|NAME=RAO VIKRAM\|NAME=WHYTE COLIN\|(IN202417013808)\|NAME=Darrah Thomas\|NAME=Rao Vikram\|NAME=Whyte Colin\|(AU2022318480)\|NAME=DARRAH, Thomas\|NAME=RAO, Vikram\|NAME=WHYTE, Colin\|(CA3227505)\|NAME=DARRAH, THOMAS, COUNTRY=US \|NAME=RAO, VIKRAM, COUNTRY=US \|NAME=WHYTE, COLIN, COUNTRY=US	(US12545576)\|7\|(US12006212)\|7\|(WO2023/007466)\|7\|(IN202417013808)\|7\|(JP2024528907)\|7\|(AU2022318480)\|7\|(CA3227505)\|7\|(US20230102312)\|7	5	10			(EP4377258)\|WO2023/007466\|(JP2024528907)\|WO2023/007466\|(BR112024001825)\|WO2023/007466\|(IN202417013808)\|WO2023/007466\|(AU2022318480)\|WO2023/007466\|(CA3227505)\|WO2023/007466		(US12545576)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=11\|Independent Claim Number: ICL=1,18\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Term Disclaimers Indicated TDI=Term Disclaimers Indicated\|Extended under 35 USC 154(b) the following days: EXTD=0\|Primary examiner: Wartalowicz Paul A\|Art Unit.: ART =1735\|\|(US20240308843)\|Number of Claims: NCL=19\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,17\|Number of Independent Claims: NICL=2\|Exemplary Claim Number: ECL=1\|Primary examiner: Wartalowicz Paul A\|Art Unit.: ART =1735\|\|(US12006212)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=11\|Independent Claim Number: ICL=1,10,20\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|Extended under 35 USC 154(b) the following days: EXTD=0\|Primary examiner: Wartalowicz Paul A\|Art Unit.: ART =1735\|\|(US20230271827)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,8,18\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|Primary examiner: Wartalowicz Paul A\|Art Unit.: ART =1735\|\|(US20230102312)\|Number of Claims: NCL=20\|Number of Drawings: NDR=9\|Number of Figures: NFG=9\|Independent Claim Number: ICL=1,8,18\|Number of Independent Claims: NICL=3\|Exemplary Claim Number: ECL=1\|\|(WO2023/007466)\|Number of Claims: NCL=67\|Extended kind: EXTK=x\|\|(JP2024528907)\|Number of Claims: NCL=67\|Request for examination: REQEXA=true\|\|(IN202417013808)\|Number of Claims: NCL=67\|\|(AU2022318480)\|Number of Claims: NCL=67\|\|(CA3227505)\|Number of Claims: NCL=20\|	(US12545576)\|Continuation of: US18/302,702 FDD=2023-04-18 [2023US-18302702]\|Continuation of: US17/815,914 FDD=2022-07-28 [2022US-17815914]\|Continuation of: US12006212 \|Provisional Appl: US63/203,814 FDD=2021-07-30 [2021US-63203814]\|Previous publication: US20240308843 A1 2024-09-19 [US20240308843]\|(US12006212)\|Continuation of: US17/815,914 FDD=2022-07-28 [2022US-17815914]\|Provisional Appl: US63/203,814 FDD=2021-07-30 [2021US-63203814]\|Previous publication: US20230271827 A1 2023-08-31 [US20230271827]\|(US20230102312)\|Provisional Appl: US63/203,814 FDD=2021-07-30 [2021US-63203814]	(EP4377258)\|ENGLISH (ENG)	(US12545576)\|Patent\|(EP4377258)\|Patent\|(US20240308843)\|Patent\|(JP2024528907)\|Patent\|(US12006212)\|Patent\|(EP4377258)\|Patent\|(BR112024001825)\|Patent\|(IN202417013808)\|Patent\|(AU2022318480)\|Patent\|(BR112024001825)\|Patent\|(US20230271827)\|Patent\|(US20230102312)\|Patent\|(CA3227505)\|Patent\|(WO202307466)\|Patent	Titre: (EP4377258)\|Systems and methods for generating hydrogen and magnetite from rock Résumé: (EP4377258)\|Systems and methods for sequestering carbon, evolving hydrogen gas, producing iron oxide as magnetite, and producing magnesium carbonate as magnesite through sequential carbonation and serpentinization/hydration reactions involving processed olivine- and/or pyroxene-rich ores, as typically found in mafic and ultramafic igneous rock. Precious or scarce metals, such nickel, cobalt, chromium, rare earth elements, and others, may be concentrated in the remaining ore to facilitate their recovery from any gangue material.	43	Abstract	gpt-4o-mini	yes	The patent describes methods for sequestering carbon through carbonation reactions involving olivine, which aligns with the topic of enhanced weathering and carbon capture.
44	JP2021075533	JP2021075533	JP7699796\|JP2022169854	102507569	JP7699796 B2 2025-06-30 [JP7699796]\|JP2022169854 A 2022-11-10 [JP2022169854]	2021-04-28	2021-04-28	2025-06-30\|2022-11-10	(JP7699796)\|2025-06-30	(JP7699796)\|2041-04-28	(JP7699796)\|How to remove carbon dioxide from the air	(JP7699796)\|PROBLEM TO BE SOLVED: To provide a method which can be executed at low cost, can substantially reduce carbon dioxide, and removes carbon dioxide in the air friendly to an environment with no risk of storing the carbon dioxide.SOLUTION: The present invention atomizes a rock containing an alkaline earth metal, immobilizes carbon dioxide to the rock by bringing acquired fine particles into contact with the air in a space as prescribed environment to mineralize carbon dioxide in the air as carbonate, and removes the carbon dioxide in the air. The invention can easily remove the carbon dioxide in the air at low cost without using chemical, and can remove qualitative carbon dioxide with little production amount of accompanying carbon dioxide. In addition, the immobilized carbon dioxide becomes carbonate harmless to environment and friendly to the environment with no risk of storing the carbon dioxide.SELECTED DRAWING: Figure 1COPYRIGHT: (C)2023,JPO&INPIT	WASEDA UNIVERSITY	(JP7699796)\|WASEDA UNIVERSITY\|(JP2022169854)\|WASEDA UNIVERSITY	COREY ADAM MYERS\|NAKAGAKI TAKAO	(JP7699796)\|Myers, Corey Adam\|NAKAGAKI Takao\|(JP2022169854)\|COREY ADAM MYERS\|NAKAGAKI TAKAO	(JP7699796)\|HATA, Masanori\|Reg. Nb: 100115842	(JP7699796)\|It is desirable that at least 5000 (or 10000) particles are analyzed for each sample of the compound.\|Table 3 confirms that the present invention works more advantageously than other technologies.\|The present invention can be advantageously used as a means for providing a technique that enables carbon dioxide in the air to be immobilized as a carbonate on a rock to reduce carbon dioxide in the air, and has high industrial applicability.\|Furthermore, the method disclosed in the non-patent document 3 is a method for simply dispersing crushed rocks on the soil surface, which is undesirable because it is difficult to estimate the amount of carbon dioxide mineralization and may adversely affect the environment.\|On the other hand, such a method does not reduce greenhouse gases because it has a large energy load and a large amount of carbon dioxide emissions.\|These transport and storage systems are too large and costly for individual companies to manufacture and operate, and there are various political, economic, and social risks associated with achieving CDR. dependent on systems that store carbon dioxide underground.\|	(JP7699796)\|1. A method for removing carbon dioxide from the air, wherein a compound (excluding a carbonate) containing at least one of Ca (calcium) and Mg (magnesium) is used. of rock to obtain fine particles of the rock; and The method includes a carbonate formation step in which the fine particles of the rock thus obtained are brought into contact with air in a space having a temperature of 15-50°C and a relative humidity of 50-100%, and carbonates are formed in the fine particles of the rock The amorphous portion of the rock is 30 mass% or less of the whole, and the fine particles of the rock have a particle diameter of 1-100 μm The fine particles of the rock are put in the tray in a state of spreading in a laminar state over the entire bottom surface of the tray, and are brought into contact with the air by placing the tray in the space A method for removing carbon dioxide from the air, characterized in that the fine particles of the rock spread in the layer have a thickness of 1 to 50 mm.\|	(JP7699796)\|An aspect of the present invention is explained below.\|The present invention provides an environmentally friendly method for removing carbon dioxide from the air, the method being implemented at a low cost, being capable of substantially reducing carbon dioxide, and being free from the risk of carbon dioxide retention.\|The present invention relates to a method for removing carbon dioxide from air. More specifically disclosed is a method for removing carbon dioxide from the air, which enables the conversion of carbon dioxide from the air into a useful and harmless state by mineralizing carbon dioxide as a carbonate.\|	(JP7699796)\|CARBON DIOXIDE(100,117)\|AIR(100,53)\|ROCK FINE PARTICLE(100,22)\|REMOVING CARBON DIOXIDE(100,14)\|DISPERSING CRUSHED ROCK(75,1)\|ROCK(54,71)\|ULTRABASIC ROCK(49,3)\|FINE PARTICLE(44,39)\|TRAY(43,13)\|CARBON DIOXIDE CONVERSION(36,1)\|CARBON DIOXIDE MINERALIZATION(35,7)\|WASTE CONCRETE(35,6)\|CARBONATE FORMATION(32,6)\|ENVIRONMENTALLY FRIENDLY(32,4)\|CARBON DIOXIDE RETENTION(30,2)\|SOCIAL RISK(30,1)\|CARBON DIOXIDE EMISSION(27,4)\|PGM TAILING MINERAL CARBONATION(27,1)\|REDUCING CARBON DIOXIDE(27,1)\|GRAVEL(26,3)\|GREENHOUSE GAS(25,1)\|CALCIUM ALUMINATE(24,9)\|PARTICLE DIAMETER(24,5)\|GROUND SURFACE(20,1)\|ROCK AMORPHIZATION(19,2)\|MINERALIZATION RATE(18,9)\|WORLD OCEAN ACIDIFICATION(18,1)\|ROCK PARTICLE(17,4)\|SLAG MINERALIZATION RATIO(17,2)\|BIBIORNITHOSPHERITE ORNITHOSPHERITE(17,1)\|MONOLITHOSPHERITE ORNITHOSPHERITE(17,1)\|MAGNESIUM OXIDE(15,19)\|SLAG RAPID MINERALIZATION(15,1)\|MAGNESIUM ALUMINOSILICATE(14,2)\|PULSATILE ROCK(14,2)\|NATURAL ROCK(13,15)\|ENTIRE BOTTOM(13,3)\|FAST MINERALIZATION REACTION(13,2)\|BASALT IC ROCK(13,1)\|CALCIUM FERROUS ALUMINATE(13,1)\|DANG ORNITHOSPHERITE(13,1)\|MACHINERY INDUSTRIALIZATION(13,1)\|MICROPARTICULATING ROCK(13,1)\|NATURAL SUPRABASIC ROCK(13,1)\|SUPRAPACEOUS ROCK(13,1)\|IRON OXIDE(12,12)\|CRYSTALLINE MINERAL(12,2)\|DEEP ROCK(12,2)\|FINE STONE PARTICLE(12,2)\|MINERALIZATION POTENTIAL(12,2)\|CO2 MINERALIZATION(12,1)\|MICRONIZING ROCK(12,1)\|ROCK MINERALIZATION PERFORMANCE(12,1)\|ROCK PARTICULATE(12,1)\|ULTRAPASCULAR STONE(12,1)\|WHOLE ROCK REACTIVITY(12,1)\|RELATIVE HUMIDITY(11,7)\|CAAL2SI2O(11,5)\|CAMGSIO(11,5)\|CALCIUM SILICATE IRON(11,3)\|ROCK COMPONENT(11,3)\|UNREACTED NUCLEAR MODEL(11,3)\|CA2SIO(10,4)\|ATOMIZED ROCK(10,1)\|ATOMIZING ROCK(10,1)\|BIOMASS COMBUSTION(10,1)\|CALCIUM FERROALUMINATE(10,1)\|EARTH CLIMATE(10,1)\|ENVIRONMENTALLY HARMLESS CARBONATE(10,1)\|LARGE ENERGY LOAD(10,1)\|MIXED CATION SILICATE(10,1)\|MOTTLED ROCK(10,1)\|NUCLEATION CRYSTAL DISTRIBUTION(10,1)\|ROCK FINE PARTICLE AMORPHIZATION(10,1)\|SILICATED MINERAL(10,1)\|ULTRAFINE ROCK(10,1)\|MORTAR(9,5)\|COMPOUND REACTION(9,2)\|MINERALIZE CARBON DIOXIDE(9,2)\|PARTICULATE SAMPLE(9,2)\|SIO CONTENT(9,2)\|CA2AL2SIO(8,3)\|CA2FE2O(8,3)\|CA2MGSI2O(8,3)\|CA3MGSI2O(8,3)\|CA3SI2O(8,3)\|CA3SIO(8,3)\|CA7MGSI4O(8,3)\|CALCIUM ALUMINOSILICATE(8,3)\|CAMGSI2O(8,3)\|IGNEOUS ROCK(8,3)\|ALKALINE MINERAL(8,1)\|ALUMINA SILICATE(8,1)\|CALCIUM SILICATE MAGNESIUM MOIETY(8,1)\|CO2 DIFFUSION(8,1)\|COMPOUND GRINDING(8,1)\|CRUSHER LOAD(8,1)\|INCUBATOR INDOOR SPACE(8,1)\|IRON SUBSTITUTION(8,1)\|MAGNESIUM ALUMINA OXIDE(8,1)\|MINERALIZATION DECREASE(8,1)\|ORE MATRIX(8,1)\|SLAG PARTICLE(8,1)\|USABLE ROCK(8,1)\|SEA(7,3)\|AMORPHOUS DIAMETER(7,2)\|CA3AL2O(7,2)\|CRYSTALLINE LAYER(7,2)\|IMMOBILIZED CARBON DIOXIDE(7,2)\|MAGNESIUM ALUMINATE(7,2)\|MGFE2O(7,2)\|OLIVINE(7,2)\|ROCK CRUSHING(7,2)\|SCRAPER(7,2)\|TRANSPORTATION(7,2)\|ALKALINE EARTH METAL(6,16)\|CARBON DIOXIDE REMOVAL(6,4)\|MANGANESE OXIDE(6,4)\|DACCS(6,3)\|ALKALI MINERAL(6,1)\|AMORPHIZATION DIAMETER(6,1)\|AMORPHOUS PHASE ACCOUNT(6,1)\|CALCIUM IRON ALUMINATE(6,1)\|CALCIUM IRON SILICATE(6,1)\|CALCIUM MAGNESIUM SILICATE(6,1)\|CALCIUM SILICATE MAGNESIUM SILICATE(6,1)\|CIRCULAR TRAY(6,1)\|CIVILIZATION(6,1)\|CO2 REDUCTION(6,1)\|CRYSTALLINE COMPOUND(6,1)\|ELAPSED DAY(6,1)\|FUTURE CO2(6,1)\|GROUND SLAG(6,1)\|IRON MOIETY(6,1)\|IRON SLAG(6,1)\|MAGNESIUM ION(6,1)\|MAJOR CHALLENGE(6,1)\|MICROPARTICLE FORMATION(6,1)\|MT SCALE(6,1)\|POTENTIAL CARBON FOOTPRINT ASSESSMENT(6,1)\|SAMPLE PARTICLE(6,1)\|STEEL SLAG(6,1)\|STORAGE SYSTEM(6,1)\|STUDY TREATMENT START(6,1)\|VOLUME INCUBATOR(6,1)\|BECCS(5,3)\|CASIO(5,3)\|OPTICAL MICROSCOPE(5,3)\|PRODUCT LAYER(5,3)\|ACCOUNTING(5,1)\|AIR CO2(5,1)\|AIR RECOVERY(5,1)\|ATOMIZATION(5,1)\|BERYLLIUM(5,1)\|BIOENERGY(5,1)\|CA CONTENT(5,1)\|CA12AL14O(5,1)\|CA3AL2SI(5,1)\|CA3FE2SI3O(5,1)\|CAFESI2O(5,1)\|CALCIUM MAGNESIUM IRON SILICATE(5,1)\|CALCIUM OXIDE MINERALIZATION RATIO(5,1)\|CARBON DIOXIDE CAPTURE(5,1)\|CARBON DIOXIDE DIFFUSION(5,1)\|CARBON DIOXIDE OXIDATION(5,1)\|CARBON DIOXIDE SHOW MINERALIZATION(5,1)\|CLASSIFICATION FUNCTION(5,1)\|CLIMATE CHANGE REPORT(5,1)\|CO2 SEQUESTRATION(5,1)\|COMPOUND DIFFUSION COEFFICIENT(5,1)\|CREATION(5,1)\|CRUSHED ROCK FINE PARTICLE(5,1)\|DEEP REGION(5,1)\|DISLOCATION(5,1)\|EXCEPTION(5,1)\|EXHAUST FUME REMOVAL(5,1)\|FACTORY(5,1)\|FE2SIO(5,1)\|FINE PARTICLE CLASSIFICATION(5,1)\|GENERATED CARBONATE(5,1)\|GLOBAL CARBON DIOXIDE(5,1)\|HUMIDITY CONDITION(5,1)\|IMAGEJ(5,1)\|IMPLEMENTATION PERIOD(5,1)\|INORGANIC COMPONENT(5,1)\|IRON ION(5,1)\|KG SCALE(5,1)\|KOMATIITE(5,1)\|LANDFILL(5,1)\|MAFIC ROCK(5,1)\|MARINE ECOSYSTEM(5,1)\|METAMORPHIC ROCK(5,1)\|MG3AL2SI(5,1)\|MICROMETER LEVEL(5,1)\|MINERALIZATION REACTION DEGREE(5,1)\|MOLAR DENSITY(5,1)\|MULTISTAGE(5,1)\|NET CARBON DIOXIDE(5,1)\|NET REDUCTION(5,1)\|PARTICLE PROCESSING(5,1)\|PARTICULATE LAYER(5,1)\|PETERSEN(5,1)\|PHOTOSYNTHESIS(5,1)\|POROSITY(5,1)\|\|(JP2022169854)\|AIR(100,63)\|REMOVING CARBON DIOXIDE(100,21)\|DISPERSING CRUSHED ROCK(93,1)\|ROCK FINE PARTICLE(92,19)\|PULVERIZED ROCK(82,4)\|ROCK(68,72)\|BRINGING FINE PARTICLE(67,1)\|CARBON DIOXIDE(57,121)\|MINERALIZATION(47,25)\|CARBONATE FORMATION(46,3)\|IMMOBILIZED CARBON DIOXIDE(46,1)\|FINE PARTICLE(45,49)\|CARBON DIOXIDE MINERALIZATION(45,8)\|WASTE CONCRETE(45,8)\|FINE PARTICLE ACQUISITION(44,1)\|QUALITATIVE CARBON DIOXIDE(44,1)\|GRAVEL(42,1)\|MINERALIZE CARBON DIOXIDE(37,4)\|PGM TAILING MINERAL CARBONATION(33,1)\|GREENHOUSE GAS(31,1)\|CALCIUM ALUMINATE(29,9)\|MINERAL(26,4)\|AMORPHOUS PHASE(25,13)\|GROUND SURFACE(25,1)\|CARBON DIOXIDE REDUCTION(24,6)\|CARBON DIOXIDE REMOVAL(24,5)\|VAPOR PHASE CARBON DIOXIDE(23,1)\|WORLD OCEAN ACIDIFICATION(23,1)\|CO2 MINERALIZATION(21,2)\|DEEPENING ROCK(21,2)\|ULTRABASAL ROCK(21,2)\|ATMOSPHERIC PRESSURE(19,1)\|ENERGY LOAD(19,1)\|MONOORTHORITE PERIDOTITE(19,1)\|ALKALINE EARTH METAL(18,19)\|MINERALIZATION RATE(18,5)\|MAGNESIUM ALUMINOSILICATE(18,2)\|PULVERIZED ROCK FINE PARTICLE(18,2)\|AMORPHOUS COMPOUND(16,4)\|FAST MINERALIZATION REACTION(16,2)\|VAPOR PHASE(16,2)\|DIPLOITE PERIDOTITE(16,1)\|MACHINERY INDUSTRIALIZATION(16,1)\|NATURAL SUPERBASIC ROCK(16,1)\|ROCK AMORPHIZATION(16,1)\|ROCK MICROPARTICLE(16,1)\|ULTRABASTITE ROCK(16,1)\|NATURAL ROCK(15,13)\|CALCIUM IRON OXIDE(15,6)\|CALCIUM SILICATE MAGNESIUM(15,3)\|CRYSTALLINE MINERAL(15,2)\|MINERALIZATION POTENTIAL(15,2)\|CAMGSI2O(14,5)\|CAMGSIO(14,5)\|GANGUE(14,5)\|MORTAR(14,5)\|CALCIUM IRON ALUMINATE(14,3)\|ELAPSED DAY(14,3)\|IRON CALCIUM SILICATE(14,3)\|SIO CONTENT(14,3)\|ADVANCING MINERALIZATION REACTION(14,1)\|HARMLESS CARBONATE(14,1)\|ORE HOST ROCK(14,1)\|ROCK MINERALIZATION PERFORMANCE(14,1)\|SLAG MINERALIZATION RATIO(14,1)\|ULTRAMAGNETIC ROCK(14,1)\|WHOLE ROCK REACTIVITY(14,1)\|RELATIVE HUMIDITY(13,7)\|ROCK COMPONENT(13,3)\|CA2SIO(12,4)\|CAAL2SI2O(12,4)\|ENVIRONMENTALLY FRIENDLY(12,4)\|LARGE SCALE EQUIPMENT(12,2)\|MICROPARTICULATION(12,2)\|PARTICLE DISTRIBUTION(12,2)\|ROCK WHOLE(12,2)\|UNREACTED NUCLEAR MODEL(12,2)\|ARTIFICIAL STONE(12,1)\|ATOMIZING ROCK(12,1)\|BIOMASS COMBUSTION(12,1)\|EARTH CLIMATE(12,1)\|EXCESS CONCRETE(12,1)\|FINE STONE PARTICLE(12,1)\|PATCHY ROCK(12,1)\|RAPID MINERALIZATION(12,1)\|CA2AL2SIO(11,3)\|CA2FE2O(11,3)\|CA3MGSI2O(11,3)\|CA3SI2O(11,3)\|CA3SIO(11,3)\|CA7MGSI4O(11,3)\|CALCIUM ALUMINOSILICATE(11,3)\|CARBON DIOXIDE EMISSION(11,3)\|GUIDELINE(11,3)\|IGNEOUS ROCK(11,3)\|OLIVINE(11,3)\|ALKALI ORE(10,1)\|ALKALINE MINERAL(10,1)\|ALUMINA SILICATE(10,1)\|COMPOUND GRINDING(10,1)\|INCUBATOR INDOOR SPACE(10,1)\|LAYERED ROCK FINE PARTICLE(10,1)\|MICROPARTICLE SAMPLE(10,1)\|MINERALIZATION DECREASE(10,1)\|PULVERIZER LOAD(10,1)\|ROCK PARTICLE(10,1)\|SLAG PARTICLE(10,1)\|ATOMIZATION(9,2)\|CA2MGSI2O(9,2)\|CA3AL2O(9,2)\|CARBON DIOXIDE DIFFUSION(9,2)\|MAGNESIUM ALUMINATE(9,2)\|MGFE2O(9,2)\|OLECITE(9,2)\|PESTLE(9,2)\|PHYLITE(9,2)\|STORAGE RISK(9,2)\|FINE PARTICLE SAMPLE(8,4)\|MANGANESE OXIDE(8,4)\|AMORPHIZED(8,1)\|CALCIUM IRON SILICATE(8,1)\|CIRCULAR TRAY(8,1)\|CIVILIZATION(8,1)\|CO2 DIFFUSION COEFFICIENT(8,1)\|CO2 REMOVAL(8,1)\|COMPOUND REACTION(8,1)\|CRYSTALLINE COMPOUND(8,1)\|DECREASING PARTICLE(8,1)\|FINE PARTICLE PERFECT DISTRIBUTION(8,1)\|GROUND SLAG(8,1)\|IMAGEJ(8,1)\|IRON MAGNESIUM SILICATE(8,1)\|MAGNESIUM ION(8,1)\|MAGNESIUM IRON SILICATE(8,1)\|MAJOR CHALLENGE(8,1)\|MT SCALE(8,1)\|PARTICULATE SAMPLE(8,1)\|POTENTIAL CARBON FOOTPRINT ASSESSMENT(8,1)\|PROMOTION(8,1)\|PULVERIZATION LAYER(8,1)\|PULVERIZED COMPOUND PARTICLE DIAMETER(8,1)\|STEEL SLAG(8,1)\|TERMINATION TREATMENT(8,1)\|ULTRABASITE(8,1)\|UNREACTED NUCLEUS MODEL(8,1)\|PARTICLE SIZE(7,12)\|BECCS(7,3)\|DACCS(7,3)\|OPTICAL MICROSCOPE(7,3)\|PRODUCT LAYER(7,3)\|CDR(7,2)\|AIR RECOVERY(6,1)\|AL2SI3O(6,1)\|ALUMINA MAGNESIUM OXIDE(6,1)\|AMORPHOUS CHANGE(6,1)\|AMORPHOUS DIAMETER(6,1)\|ARBITRARY AREA TRAY(6,1)\|ATMOSPHERIC CARBON DIOXIDE(6,1)\|AVAILABLE ROCK(6,1)\|BASALITE(6,1)\|BERYLLIUM(6,1)\|CA CONTENT(6,1)\|CA3FE2SI3O(6,1)\|CAFESI2O(6,1)\|CAFESIO(6,1)\|CALCIUM OXIDE MINERALIZATION RATIO(6,1)\|CARBON DIOXIDE RECOVERY(6,1)\|CARBON DIOXIDE RETENTION(6,1)\|CLASSIFICATION FUNCTION(6,1)\|CLIMATE CHANGE REPORT(6,1)\|CO2 SEQUESTRATION(6,1)\|CRUSHING(6,1)\|DANORITE(6,1)\|DISARRANGEMENT(6,1)\|DOLERITE(6,1)\|EMITTED CARBON DIOXIDE(6,1)\|EXCEPTION(6,1)\|FACTORY(6,1)\|FE2SIO(6,1)\|GENERATED CARBONATE(6,1)\|GLOBAL CARBON DIOXIDE(6,1)\|GLOBAL ENVIRONMENT PROTECTION(6,1)\|GROUP REACTION(6,1)\|IMPLEMENTATION MENSTRUATION(6,1)\|INORGANIC COMPONENT(6,1)\|IRON CALCIUM MAGNESIUM SILICATE(6,1)\|IRON ION(6,1)\|KG SCALE(6,1)\|KOMACHIITE(6,1)\|LANDFILL(6,1)\|MAFIC ROCK(6,1)\|	(JP7699796)\|1. A method for removing carbon dioxide from the air, wherein a compound (excluding a carbonate) containing at least one of Ca (calcium) and Mg (magnesium) is used. of rock to obtain fine particles of the rock; and The method includes a carbonate formation step in which the fine particles of the rock thus obtained are brought into contact with air in a space having a temperature of 15-50°C and a relative humidity of 50-100%, and carbonates are formed in the fine particles of the rock The amorphous portion of the rock is 30 mass% or less of the whole, and the fine particles of the rock have a particle diameter of 1-100 μm The fine particles of the rock are put in the tray in a state of spreading in a laminar state over the entire bottom surface of the tray, and are brought into contact with the air by placing the tray in the space A method for removing carbon dioxide from the air, characterized in that the fine particles of the rock spread in the layer have a thickness of 1 to 50 mm.\|2. The method for removing carbon dioxide in the air described in claim 1 is characterized in that the rock contains at least one kind of compound selected from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|3. The method for removing carbon dioxide in the air described in Claim 1 or Claim 2 is characterized in that the rock contains at least one compound in the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate in an amount of at least 5 mass% of the total amount of the rock.\|4. The method for removing carbon dioxide in the air described in any of claims 1 to 3 is characterized in that the rock contains at least one kind of ultra-basic rock, basic rock, slag and waste concrete.	(JP7699796)\|TECHNICAL FIELD\|[0001] The present invention relates to a method for removing carbon dioxide from air. More specifically disclosed is a method for removing carbon dioxide from the air, which enables the conversion of carbon dioxide from the air into a useful and harmless state by mineralizing carbon dioxide as a carbonate.\|BACKGROUND ART\|[0002] It is obvious that carbon dioxide emitted into the atmosphere is the cause of global warming, which has been a problem in recent years. Reducing such carbon dioxide emissions is a major challenge in protecting the global environment.\|[0003] Carbon dioxide is naturally captured from the atmosphere through biological processes such as photosynthesis by plant life on land and in the ocean, but the concentration of carbon dioxide in the atmosphere continues to rise. Carbon dioxide is also said to be a factor in the acidification of the world's oceans, which poses a threat to marine ecosystems. On the other hand, systems for fixing and removing exhaust fumes from factories and carbon dioxide (CO2) gas in the atmosphere have been proposed in various ways (for example, see Patent Document 1, etc.). ).\|[0004] Net reduction of global carbon dioxide (CO2) concentrations to eliminate or reduce atmospheric CO2 is It is referred to as NET (Negative Emission Technology) or Carbon Dioxide Removal (CDR.) and various technologies are available (see, for example, Non-Patent Document 1 or Non-Patent Document 3). ).\|[0005] The carbon dioxide emitted must be removed from the atmosphere to stabilize the Earth's climate within a range compatible with modern civilization. Also, in general, the techniques described in the literature described above should be applied to biological systems (e.g., retention of carbon dioxide in soil, plants, or the ocean). ) or highly industrialized machinery that filters carbon dioxide from the air, liquefies it, and stores it underground. And, there was a tendency that chemicals, high temperature and special reactor were required for industrial process which depended on such machinery.\|CITATION LIST\|PATENT LITERATURE\|[0006] Special Report No. 2013-504424\|NON PATENT LITERATURE\|[0007] Nduagu, E., Bergerson, J. and Zevenhoven, R., 2012. Life cycle assessment of CO2 sequestration in magnesium silicate rock A comparative study. Energy Conversion and Management, 55, pp.116-126.\|Ncongwane, M.s., Broadhurst, J.L. and Petersen, J., 2018. Assessment of the potential carbon footprint of engineered processes fwor the mineral carbonation of PGM tailings. International Journal of Greenhouse Gas Control, 77, pp.70-81.\|Keller, d.P., Lenton, A., Littleton, E.w., Oschlies, A., Scott, v. and Vaughan, N.E., 2018. The effects of carbon dioxide removal on the carbon cycle. Current climate change reports, 4(3), pp.250-265.\|DISCLOSURE\|TECHNICAL PROBLEM\|[0008] Carbon dioxide mineralization in rocks occurs naturally over hundreds of thousands of years. However, conventional methods to promote the reaction are high temperature and high pressure, or by adding chemicals. On the other hand, such a method does not reduce greenhouse gases because it has a large energy load and a large amount of carbon dioxide emissions.\|[0009] Concretely, the technology disclosed in the non-patent document 1 has a problem that the substantial reduction in carbon dioxide amount is reduced because carbon dioxide is reacted with carbon dioxide under high temperature and high pressure conditions. In addition, the technology disclosed in Non-Patent Document 2 requires the addition of chemicals and background emissions during its production (e.g., carbon dioxide emissions related to the creation, transportation, termination and disposal of chemicals and additives). As with the technology disclosed in Non-Patent Document 1, substantial CO2 reductions were reduced by the use of CO2-P-P (Carbon Dioxide Reduction Method).\|[0010] Furthermore, the method disclosed in the non-patent document 3 is a method for simply dispersing crushed rocks on the soil surface, which is undesirable because it is difficult to estimate the amount of carbon dioxide mineralization and may adversely affect the environment.\|[0011] The direct removal of carbon dioxide from the atmosphere is only a part of the total amount of carbon dioxide removal (CDR.) that has already been released, which is in line with the climate change reduction target. The removed carbon dioxide must be transported to the appropriate location for disposal and stored deep underground in certain geological structures. These transport and storage systems are too large and costly for individual companies to manufacture and operate, and there are various political, economic, and social risks associated with achieving CDR. dependent on systems that store carbon dioxide underground.\|[0012] The present invention provides an environmentally friendly method for removing carbon dioxide from the air, the method being implemented at a low cost, being capable of substantially reducing carbon dioxide, and being free from the risk of carbon dioxide retention.\|TECHNICAL SOLUTION\|[0013] The method for removing carbon dioxide from the air according to the present invention is a method for removing carbon dioxide from the air, wherein a compound (excluding a carbonate) contains at least one of Ca (calcium) and Mg (magnesium). of rock to obtain fine particles of the rock; and The method includes a carbonate formation step in which the fine particles of the rock thus obtained are brought into contact with air in a space having a temperature of 15-50°C and a relative humidity of 50-100%, and carbonates are formed in the fine particles of the rock The amorphous portion of the rock is 30 mass% or less of the whole, and the fine particles of the rock have a particle diameter of 1-100 μm The fine particles of the rock are put in the tray in a state of spreading in a laminar state over the entire bottom surface of the tray. The rock is characterized in that the rock particles which are brought into contact with the air by placing the tray in the space and spread in the layer form have a thickness of 1 to 50 mm.\|[0014] The method for removing carbon dioxide from the air is characterized in that the rock contains at least one compound from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|[0015] The method for removing carbon dioxide from the air is characterized in that the rock contains, in a total amount, 5 mass% or more of at least one compound from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|[0017] The method for removing carbon dioxide from the air is characterized in that the rock contains at least one member selected from among ultra-basic rock, basic rock, slag and waste concrete.\|ADVANTAGEOUS EFFECTS\|[0020] The present invention secures carbon dioxide to a rock and removes carbon dioxide from the air by atomizing the rock containing an alkaline earth metal, bringing the obtained particulates into contact with air in a space having a predetermined environment, and mineralizing carbon dioxide in the air as a carbonate.\|[0021] Consequently, the present invention can easily remove carbon dioxide from the air at low cost without using a chemical or using a large-scale facility, etc., and can substantially reduce carbon dioxide because the amount of carbon dioxide generated is small. In addition, there is no need of storing carbon dioxide, and there is no risk in such storage, and the immobilized carbon dioxide becomes a carbonate harmless to the environment, and can be reused together with rocks, so that it is also environmentally friendly.\|DESCRIPTION OF DRAWINGS\|[0022] This chart (Graph 1) shows the change in the mineralization effect (mineralization rate (%)) of carbon dioxide in the atmosphere as a result of measuring the number of elapsed days as 14 days.\| This chart (Graph 2) shows the change in the mineralization effect (mineralization rate (%)) of carbon dioxide in the atmosphere as the number of months in December (one year).\|DESCRIPTION OF EMBODIMENTS\|[0023] An aspect of the present invention is explained below. The method for removing carbon dioxide from the air according to the present invention comprises atomizing a rock containing an alkaline earth metal ((I) atomization step) and bringing the atomized rock into contact with the air in a space having a specific environment Carbon dioxide in the air is mineralized and fixed by using carbon dioxide in the air as a carbonate ((II) carbonate formation process) to remove the carbon dioxide from the air.\|[0024] Step (A): In the step of atomizing, the rock is pulverized to obtain fine particles.\|[0025] (A-1) About rocks: First, I will explain available rocks. Any of natural and man-made rocks can be used as rocks if they are formed from the compounds, etc. shown below. In the present invention, the term "compound" also includes "mineral".\|[0026] Usable rocks are, for example, 0-100°C temperature, suitable moisture (for example, relative humidity of reaction environment is 50-100%, etc.). It is required that the formation of carbonate by reaction with gas phase carbon dioxide under atmospheric pressure is thermodynamically possible. The term "thermodynamically" is taken to mean that 0-dimensional calculation conditions are considered and meso-scale structures are not considered.\|[0027] The rocks usable in the present invention are so-called slags (steel slags, iron slag, etc.), which are composed of a substance containing a mineral component of an ore matrix, etc., which has been separated by melting from a metal to be metallurgically measured, when smelting the metal from the ore, etc., as rocks containing a compound containing an alkaline earth metal. In addition, concrete that was originally used for buildings, etc., such as demolished concrete that is created when the building itself is no longer necessary or when the building, etc. that used the building, etc. is demolished, and surplus concrete itself that occurs when the building, etc. is built, etc. It includes waste concrete (concrete waste) which is concrete, etc., expected to be disposed of in the future, and it is preferable to use these slag and waste concrete. Since the carbonate does not react with carbon dioxide in the air to further become a carbonate, it is excluded from compounds containing alkaline earth metals.\|[0028] The rock contains a compound containing an alkaline earth metal. That is, compounds such as Ca (calcium), Mg (magnesium), Be (beryllium), Sr (strontium), Ba (barium), and Ra (radium), which are alkaline earth metals, are cited, but it is preferable to use a compound of Ca (calcium) and Mg (magnesium), which is largely contained in natural rocks.\|[0029] The following is an example of a compound containing an alkaline earth metal. First, an oxide of a single alkaline earth metal is cited. For example, calcium oxide (CaO) which is an oxide of calcium, magnesium oxide (MgO) which is an oxide of magnesium, and the like can be used.\|[0030] Although barium oxide (BaO), which is an oxide of barium, strontium oxide (SrO), etc., which is an oxide of strontium, etc., it is preferable to use calcium oxide (CaO), magnesium oxide (MgO), which is an oxide of magnesium, etc.\|[0031] Other oxides include magnesium/iron oxides (MgFe2O4, etc.), calcium/iron oxides (Ca2Fe2O5, etc.), magnesium aluminate (magnesium alumina oxide) (MgAl2O4, etc.), calcium aluminate, and calcium oxide. An oxide such as calcium ferroaluminate can be used. For example, calcium aluminate such as Ca3Al2O6, Ca12Al14O33 or calcium iron aluminate such as Ca4Al2Fe2O10 can be used.\|[0032] As the compound, for example, calcium silicate can be used. For example, a calcium silicate such as Ca2SiO4, Ca3Si2O7, Ca3SiO5, CaSiO3 can be transferred.\|[0033] As the compound, for example, magnesium silicate or magnesium aluminosilicate can be used. For example, magnesium silicate such as MgSiO3 and Mg2SiO4 or magnesium aluminosilicate such as Mg3Al2Si3O12 can be used.\|[0034] As the compound, for example, calcium silicate magnesium can be used. For example, a calcium silicate magnesium such as CaMgSiO4, Ca3MgSi2O8, Ca7MgSi4O16, CaMgSi2O6, Ca2MgSi2O7, etc., can be used.\|[0035] As the compound, for example, calcium aluminosilicate can be used. For example, calcium aluminosilicate such as CaAl2Si2O8, Ca2Al2SiO7, Ca3Al2Si3 O12, etc., can be used.\|[0036] As the compound, for example, calcium silicate iron can be used. For example, CaFeSiO4, (Ca/Fe)SiO3, (Ca/Fe)2SiO4, Ca3Fe2Si3O12, CaFeSi2O6, Ca0.82Fe0.18SiO2, etc., Ca(Fe/Mg)Si2O6, Calcium iron silicate, calcium magnesium iron silicate, magnesium iron silicate, etc. can be used.\|[0037] For example, calcium silicate iron can be CaXFe2-XSiO4 (0<X<2). A compound obtained by substituting iron for the calcium silicate magnesium moiety or a compound obtained by substituting magnesium for the iron moiety of the calcium silicate iron may also be used.\|[0038] In the application of the present invention to a compound containing an alkaline earth metal, including the above-described compound, the reactivity of the original compound (i.e., difficulty in mineralizing carbon dioxide due to contact with carbon dioxide or difficulty in mineralizing carbon dioxide. This suggests that there is a difference in the reactivity when pulverized and atomized.\|[0039] Figures 1 and 2 show that the compounds listed in Figures 1 and 2 are selected from the above compounds, and pulverized so that their particle sizes are less than 3 μm. Assuming the temperature is 30°C and the relative humidity is 90%, the change in the mineralization effect (mineralization ratio (%)) of carbon dioxide (carbon dioxide concentration: 415ppm) in the atmosphere for the target compound is estimated to be 14 days old (the compound shown in Figure 1). The figure shows the results when the number of months elapsed is measured as December (one year) (the compound listed in Figure 2). Fig. 1 is referred to as "graph 1" and Fig. 2 is referred to as "graph 2".\|[0040] The mineralization ratio (%) is the actual mineralization amount of each compound relative to the CO2 (carbon dioxide) mineralization amount potential represented by formula (I) (see formula (II)). ).\|[0041] The CO2 mineralization potential indicates the amount of mineralization that is ideally achievable, and the mineralization rate (%), which is the ratio of the actual amount of mineralization to the potential, is an index indicating the degree of ease of mineralization (mineralization reaction).\|[0042] \|[0043] \|[0044] From Figures 1 and 2, the compounds listed in Figure 1 (CaO, MgO, Ca2SiO4, CaSiO3) have excellent reactivity and are shown to be highly reactive. (In Fig. 2, the lines of Mg2SiO4 and MgSiO3 results almost overlap. ). In addition to Figures 1 and 2, Table 1 shows that the CO2 mineralization potential (kg-CO2/kg) is determined by selecting the compounds listed in Table 1 from the above compounds. If the particle size of the crushed compound is 1 to 3 μm, the mineralization rate (%) after 1 year when it is 5 to 10 μm (Table 1 abbreviates "mineralization rate", but it is agreed with the mineralization rate (the same as the others). ) is shown.\|TABLE 1\|[0045] \|[0046] Although the above compound (mineral) is an example, it can be confirmed that the mineralization ratio of calcium oxide (CaO), magnesium oxide (MgO), calcium/iron oxide, calcium aluminate, and calcium silicate, which are oxides of alkaline earth metals, is high.\|[0047] From this result, it is preferable that the rocks used in the present invention contain these compounds, which are referred to as "Group 1" in Table 1 (corresponding to "Group 1" described below). ).\|[0048] 1, 2, and Table 1 indicate that these compounds have high mineralization rates (fast mineralization reaction) and, when contained in rocks, can form carbonates efficiently by contact with carbon dioxide in the air.\|[0049] According to the results of Table 1, etc., the compounds can be divided into the following groups 1 to 3. Each group is considered to have the following characteristics regarding mineralization.\|[0050] In addition, natural rocks, slag, waste concrete, etc., often contain compounds other than the above compounds, i.e., compounds not containing alkaline earth metals. For example, silicon oxide (SiO2), aluminum oxide (alumina) (Al2O3), aluminosilicate, iron oxide (FeO, Fe2O3, Fe3O4), and aluminum oxide are oxides. Compounds (minerals) such as manganese oxide (MnO), iron silicate (FeSiO3, Fe2SiO4), carbonate, and alkali minerals are enumerated. All of these are pulsate stones, which are essentially unnecessary compounds (ores).\|[0051] Compounds such as these compounds that do not contain alkaline earth metals, such as calcium and magnesium, do not form carbonates even when ground and brought into contact with carbon dioxide under prescribed conditions (Group 4). ). The group 4 also contains a compound which cannot form a carbonate under a predetermined condition.\|[0052] Based on the results of Table 1 and other data, Groups 1 through 4 are defined as follows by the degree of mineralization reaction.\|[0053] Group 1: Carbon dioxide mineralization is roughly completed (>95%) within 1 year if the particle size is crushed to 1 to 3 μm. When the particle size is crushed to 5 to 10 μm, it is 60% or more. Refers to compounds (minerals) that are considered possible (highly reactive compounds). For example, calcium oxide (CaO), Magnesium oxide (MgO), oxide of calcium/iron oxide (Ca2Fe2O5, etc.), Ca3Al2O6, Ca12. The composition contains at least one compound among calcium aluminate such as Al14O33 and calcium silicate such as Ca2SiO4, Ca3Si2O7, Ca3SiO5, and CaSiO3 The compounds, etc. listed in Group 1 in Table 1 are enumerated. Further, the compounds containing an alkaline earth metal, as described in the present invention, such as these compounds and the compounds of the second group, include compounds that are partially substituted with other elements and that are construed to belong to these compounds. Concretely, a compound such as calcium silicate, magnesium silicate or calcium magnesium silicate wherein a part of calcium ion or magnesium ion is replaced by iron ion may be used.\|[0054] Group 2: Compounds that, even when milled to 1 to 3 μm in particle size, are considered to have a carbon dioxide mineralization rate of 10 to 95% within 1 year (compounds with normal reactivity). For example, calcium ferrous aluminate such as Ca4Al2Fe2O10, magnesium silicate such as MgSiO3 and Mg2SiO4, calcium aluminosilicate such as CaMgSiO4, Ca3MgSi2O8, Ca2MgSi2O7, Ca7MgSi4O16, CaMgSi2O6, calcium silicate magnesium silicate such as Ca2Al2SiO7, CaAl2Si2O8, etc., and MgAl2O4. The term "A-" refers to amorphous (amorphous) compounds such as oxide (magnesium aluminate), magnesium/iron oxide such as MgFe2O4, A-CaMgSiO4, A-Ca2MgSi2O7, A-Ca3Si2O7, and A-CaSiO3. The same applies hereinafter. Table 1, Group 2 (2). Compounds listed in the table above are examples.\|[0055] Group 3: Refers to compounds (compounds with slightly lower reactivity) that are considered to have a carbon dioxide mineralization rate of less than 10% within 1 year, even if the particle size is crushed to 1 to 3 μm. For example, Group 3 (3 in Table 1 includes A-Ca3SiO5, A-CaAl2Si2O8, A-Ca2SiO4, A-MgSiO3, A-Ca2Al2SiO7, A-Ca3MgSi2O8, A-Ca7MgSi4O16, A-Ca2Fe2O5, A-CaMgSi2O6, etc. Compounds listed in the table above are examples.\|[0056] Group 4: Alkaline earth metals (calcium, magnesium, etc.) It is a compound that does not contain carbonic acid (including thrombophiles), or that is thought to be unable to form carbonic acid under ambient conditions. (Chemical compounds that cannot be expected to react). For example, silicon oxide (SiO2), aluminum oxide (alumina) (Al2O3), iron oxide (FeO, Fe3O4, Fe2O5, etc. Examples include manganese oxide (MnO), iron silicate (FeSiO3, Fe2SiO4), carbonate, and alkaline minerals.\|[0057] As the rocks to be applied to the method of the present invention, the ratio of the groups 1 to 4 is considered to be important. In the above group, the reactivity is highest when the group 1 is considered as a single compound and lowest when the group 4 is considered as a single compound (reactivity is Group 1>Group 2>Group 3>Group 4. ).\|[0058] It goes without saying that the composition of the rocks used is better if they have a high content of compounds belonging to the group with high reactivity. The range of the content of each group is shown below, but as described below, reactivity includes the presence of other components of the rock (natural rocks include the presence of pulsels, etc.). Therefore, the following range is only one criterion, because it depends on the particle size (particle size) obtained in the particle processing, the carbon dioxide concentration of the air in contact, etc.\|[0059] I would like to expect that the compounds belonging to Group 1 are present as much as possible in rocks compared with the compounds of other groups, but in the case of natural rocks, there are many cases where it is not known unless it is mined, so it cannot be determined uniformly.\|[0060] In consideration of such circumstances, the following compounds belong to Group 1: (i) Calcium oxide, Magnesium oxide, Calcium/Iron oxide, Calcium aluminate, Calcium silicate, etc. The rock preferably contains not less than 5% by mass relative to the whole rock, more preferably not less than 10% by mass, and particularly not less than 15% by mass. The more compounds in Group 1, such as all of the rocks (100% by mass) or more than 90% by mass of the whole rock, the better the mineralization performance of the rock. The content which can actually be expected is limited to about 25 mass%, and it is considered that 5 to 20 mass% should be contained. In addition, the compounds belonging to Group 1 are generally contained in an amount of 5 to 20 mass% relative to the total amount of the natural rocks when the compounds of Group 1 are present. In the case of slag, waste concrete, etc., the content is often 0 to 90 mass%.\|[0061] Compounds belonging to Group 2 (excluding those amorphized in Table 1) In the case of a rock containing a compound belonging to Group 1, it is preferable to contain as much of the remainder (generally 80-100 mass% of the remainder) excluding the compound belonging to Group 1 as possible, because the rock does not want to contain the compound belonging to Group 3 and Group 4 described below as much as possible.\|[0062] On the other hand, when not containing a compound belonging to Group 1, the compound belonging to Group 2 is preferably contained in an amount of 50 mass% or more, preferably in an amount of 70 mass% or more, and particularly preferably in an amount of 70-100 mass%, with respect to the whole rock. In the case of natural rocks, the amount of compounds belonging to Group 2 is approximately 70-100% by mass in total relative to the whole rock (in the case of no compounds belonging to Group 1, the amount of total compounds belonging to Group 1 is about 70-100% by mass in the case of natural rocks. When present, it is generally contained in an amount of 0 to 25 mass%. When used in slag, waste concrete, etc., it is often contained in an amount of 0 to 30 mass%.\|[0063] It is preferable that the compounds belonging to Group 3, Group 4 are not present as much as possible.\|[0064] When the rock is a natural rock, for example, magnesium oxide (MgO), calcium oxide (CaO), magnesium silicate, calcium silicate magnesium, and magnesium iron silicate can be mainly used in the present invention.\|[0065] Natural rocks, for example, igneous rocks, sedimentary rocks, metamorphic rocks, etc., are considered, but igneous rocks are preferably used. Although the igneous rock may be a deep rock, volcanic rock, etc., it is preferable to use the deep rock.\|[0066] From the content of SiO2, the rock is acidic (generally, the content of SiO2 exceeds 66 mass% of the whole). The SiO2 content is 52-66% by mass. Rock mass: 45-52% by mass (basic rock), 45-52% by mass (suprabasic rock), 45% by mass or less (basic rock). ) can be listed. In the present invention, it is preferable to use a suprabasic rock or a basic rock, and particularly preferable to use a suprabasic rock.\|[0067] Suprabasic rocks, also called suprapaceous rocks, are generally composed of ornithospherite, dang ornithospherite, serpentine, ornithospherite ornithospherite, monolithospherite ornithospherite, bibiornithospherite ornithospherite, komatiite, etc. Basic rocks are also called mafic rocks, and generally consist of mottled rocks, basaltic rocks, drylights, etc.\|[0068] The basic rock is composed mainly of magnesium silicate (magnesium silicate) and CaSi such as MgSiO3 (olivine) and Mg2SiO4 (olivine). Contains mgSi2O6 (pyroxite), and may also contain a silicated mineral such as CaAl2Si2O8. The magnesium silicate belongs to the group 2, and the mineralization reaction is not so fast.\|[0069] On the other hand, magnesium oxide (MgO) belonging to Group 1 and very fast mineralization reaction (generally considered to be about 0 to 10 mass% in general, but it is not limited to this range) is appropriate for the ultra-basic rock. It is considered that the total amount of the compounds in Group 1 is about 5 to 20 mass%. In addition, it is a natural rock suitable for mineralization because silica (SiO2) and alumina silicate are hardly contained in the suprabasic rock. In addition, ultrafine rocks are natural rocks that are widely available in large quantities.\|[0070] The basic rock is composed mainly of CaAl2Si2O8 and other suitable compounds. and CaMgSi2O6 (pyroxene). Magnesium silicate (magnesium silicate) such as MgSiO3 (talc), Mg2SiO4 (talc), etc. are also included.\|[0071] Rocks containing many amorphous (amorphous) compounds (rocks with a large amount of amorphous phase) have low reactivity and often interfere with mineralization. Since they envelop other crystals and are involved in the amorphous phase, they are connected to each other (it is important to advance the mineralization reaction). (This will prevent you from doing so.\|[0072] In the state of the rock before grinding, the amorphous portion of the rock (the rock having a large amount of an amorphous phase) containing a large amount of an amorphous compound is generally preferred to be 30 mass% or less. If the proportion of amorphous (amorphous) parts is 30 mass% or less, it is considered that completely enclosing the crystals is suppressed, even if the amorphous phase (amorphous part) may occupy the space between the crystalline minerals. The above range includes the presence of other components of the rock (natural rock includes the presence of pulsatile rocks, etc.). Therefore, the range of exposure depends on the particle size (particle size) and the carbon dioxide concentration of the air in contact with the particles.\|[0073] (A-2) Pulverization: In the case of natural rocks, the rock is mined and then pulverized to form fine particles. In the micronization process, the crystal state of each rock-forming compound is maintained (amorphous). (This is important.\|[0074] When the compound constituting the rock is pulverized into fine particles, the smaller the particle size, the larger the surface area of the fine particles and the larger the contact surface with air (carbon dioxide). However, if the particle size is too small, the rock becomes amorphous and the reactivity to mineralization decreases.\|[0075] Of the above compounds, the compounds listed in Table 2 are selected, and the approximate particle size (amorphous diameter) to be amorphous (amorphous diameter) when pulverized into fine particles is listed in Table 2. In addition, "grinding efficiency of each compound" and "effective rate of mineralization" are also listed in Table 2. In addition, the amorphization diameter shown in Table 2 is only a guide, and it does not reliably amorphize if it is below this diameter.\|TABLE 2\|[0076] \|[0077] The time t required for the reaction of the fine particles having a radius of R(m) to reach the depth δ is expressed in formula (III). The concentration of calcium (Ca) and magnesium (Mg) in a solid is ρ, the vapor phase concentration of CO2 is Cg, and the diffusion coefficient of ions through the product layer is D (m2/s).\|[0078] \|[0079] t: Time (sec) ρ: Sum of molar density of magnesium (Mg) and calcium (Ca) in rock (moles/m3-rock) R: Radius of fine particles (m) D: Concentration of CO in the compound Diffusion coefficient of CO2 (m2/s)Cg: CO2 molar concentration in gas phase (moles/m3-gas) δ: Reaction depth (m)\|[0080] On the other hand, if the radius (particle size) of the fine particles is too large, it takes a very long time for all of the fine particles to react, which is also undesirable. According to the unreacted nuclear model, the reaction rate is considered to be inversely proportional to the cube of the diameter of the particles. For example, if the crushing result is 6 μm as a result of assuming 3 μm, the reaction is considered to be 8 (23) times slower.\|[0081] The diffusion coefficient, D, represents the rate of CO2 diffusion through the product layer in the unreacted nuclear model (m2/s), and does not directly represent the mineralization rate of carbon dioxide because of other factors. Since diffusion through the product layer is a rate-limiting step of pneumonialization of CO2, a large diffusion coefficient D actually indicates a mineral that rapidly mineralizes carbon dioxide.\|[0082] The outer diameter (particle size) of the fine particles is determined by the mass of the compound belonging to the above group 1 relative to the total fine particles of the rock obtained. It is considered that the reaction proceeds without crushing the rock more finely than necessary, and that the generation of carbon dioxide by energy loss or crushing can be suppressed, and in addition, the amorphization of the rock (compound) can be suppressed.\|[0083] On the other hand, the reactivity of the whole rock is determined by the type of other components of the rock (natural rock includes the presence of pulsatile rocks, etc.). The composition of the rock may also be referred to as the "rock element", and the composition and composition of the crystalline layer and the amorphous phase, the relationship between the crystalline layer and the amorphous phase, and other factors such as the amount of carbon dioxide oxidation (hereinafter referred to as the "rock element") may also be used. The range of particle size of the crushed rock is also affected by these factors.\|[0084] In view of these facts, when microparticulating rocks, the particle size of the fine particles is generally preferably 100 μm or less (more preferably 50 μm or less, more preferably 25 μm or less, more preferably 10 μm or less. In consideration of the rock elements, appropriate selection may be made, for example, within the range of particle sizes of 1-25 μm, 1-20 μm, 1-10 μm, 1-5 μm, 1-3 μm, etc. For example, when a first group of highly reactive compounds is contained, the particle size may be 1-25 μm (preferably 1-10 μm).\|[0085] If the particle size is 1 to 3 μm, the surface area is large and good reactivity can be expected, but as shown in Table 2, if the particle size is made too small, amorphization may progress and the reactivity may actually become poor. Therefore, it is preferable to limit the particle size of 1 to 3 μm to about 1 to 10 μm or less with the target of 1 to 3 μm. Regarding the particle size of the fine particles, for example, the fine particles of the crushed rock can be spread so as not to overlap, the image acquired by the optical microscope or the like can be analyzed by a computer, and the particle diameter (particle diameter) and shape of the complete distribution of the fine particles can be determined (preferably, the maximum particle diameter is adopted. ). It is desirable that at least 5000 (or 10000) particles are analyzed for each sample of the compound.\|[0086] The rock crushing operation in the micronization can be performed by using a conventionally known crushing means, but, for example, it is preferable to perform the rock by using vertical roller mill, high pressure grinding rolls, etc. It should be noted that ball mills generally have low energy efficiency and tend to become amorphous.\|[0087] In the case of simply atomizing the rock, the rock may be put into a mortar and crushed by using a mortar and a scraper to obtain a desired particle size. In the crushing of rocks by mortar and mortar, for example, it is possible to achieve a very low degree of amorphization by separating very small fine particles that are expected to have been amorphized when they are produced and carrying out a minimum amount of crushing to achieve a desired particle size.\|[0088] Rock crushing prevents amorphization, reduces particle distribution (size distribution of fine particles) as much as possible, minimizes energy consumption (energy consumption generates carbon dioxide, and substantial carbon dioxide reduction is reduced. (3) should be taken into account. These are considered to be particles that have become too small (amorphous) while grinding, for example, using high-pressure grinding. Also, the load of the crusher can be reduced (energy efficiency can be increased) by separating. (This will be retained for the purpose of separation.) On the other hand, the low-pressure grinding (low-pressure grinding) is preferably ground by a vertical roller mill, which is considered to be an aspect of the high-pressure grinding means, because the supplied energy causes dislocation (amorphization) of the crystal structure and generation of heat and sound (energy loss).\|[0089] It is preferable to reduce (narrow) the particle distribution in rock crushing as much as possible. By narrowing the particle distribution, the air to be contacted to mineralize carbon dioxide diffuses into the particulate layer.\|[0090] Such diffusion is an important factor in CO2 mineralization, and it is considered inefficient that the wide particle distribution reduces the porosity between particles, and only the upper part of the ground layer comes into contact with CO2. Less diffusion means that the rock is spread into a thinner layer (the rock layer becomes thinner. It means that it is necessary. The thinning of the rock layer is undesirable because it reduces the amount of rock that can be processed per unit volume of the equipment and at the same time increases the number of sheets per unit rock, which increases the cost.\|[0091] A commercial air classifier or a sieve, etc., may be used for classification. A pulverizer having a classification function may also be used. The particle size distribution is performed by using a conventional technique (for example, measuring the classified fine particles by using an optical microscope equipped with a computer vision operated by commercial software). (You can use it to do this.\|[0092] For example, as also described in CaMgSiO4 in Table 1, there are cases where the compound that has become amorphous as a result of microparticle formation mineralizes CO2 more rapidly than a compound that is not amorphous (crystalline compound). In this case, since the structure of the amorphous compound changes depending on the ratio of the cation to the silica, certain compositions such as CaMgSiO4 favorably react with carbon dioxide even in the case of an amorphous structure and mineralization proceeds.\|[0093] On the other hand, such cases are an exception, and from the point of view of engineering, you will never find pure minerals, and there is always a certain degree of mixing and variation in composition. Therefore, the significant reduction in carbon dioxide mineralization associated with most amorphous compounds outweighs the small performance gains of some compounds. In other words, it is preferable to avoid amorphous compounds because the reaction rate with carbon dioxide and the rate of mineralization are likely to be very low.\|[0094] Further, it is preferable that the rock fine particles obtained by the micronization step are not present as much as possible in the rock fine particles, because the mineralization reaction cannot be expected for the group 4 (compound not expected to react) originally contained in the rock fine particles due to the amorphization of the rock or the amorphization of the rock fine particles together with the micronization. These are preferably about 80 mass% or less in total, and are particularly preferably 50 mass% or less.\|[0095] (B) Carbonate formation process: Fine particles of the rock obtained are brought into contact with air in a predetermined space, whereby carbonates are formed in the fine particles. In other words, carbon dioxide in the air reacts with the fine particles of the rock composed of the above composition, and carbonates (mainly carbonates such as calcium and magnesium) are formed on the surface of the fine particles or in the inside thereof. As a result, carbon dioxide in the air is removed.\|[0096] The space shall be in a state where air is constantly stable (such as stably supplying air containing carbon dioxide and maintaining the conditions described below for the period of implementation, etc.). However, such a stable state can be easily and reliably formed, and it is preferable to use the stone in the room. The space is preferably a closed space capable of supplying air at a certain frequency by ventilation or the like.\|[0097] The introduced air refers to air in general that contains carbon dioxide, for example, the atmosphere (carbon dioxide content is considered to be about 400 to 450 ppm. All gases that are considered to contain carbon dioxide (CO2), such as exhaust gas, can be used. There are also no restrictions on the CO2 concentration of the air in question.\|[0098] The space is conditioned to have a temperature of 15 to 50°C and a relative humidity of 50 to 100%. Both the temperature condition and the humidity condition are within the aforementioned ranges, so that carbon dioxide is mineralized efficiently. The temperature in the space is preferably 20-40°C, and is particularly preferably 30-35°C. The relative humidity is preferably 60-95%.\|[0099] The flow rate of air containing carbon dioxide in a space can be appropriately determined according to the concentration of carbon dioxide, the type and composition of rocks. For example, a natural suprabasic rock (ultrapascular stone) is used as a rock, and the air to be carbon dioxide removed is used as the atmosphere (the carbon dioxide content is at the same level as described above). In this case, it is preferable that the exposure rate be approximately 1 to 100mm/sec, and particularly preferably 1 to 10mm/sec. Since the fine particles of the rock have a small particle diameter and are pulverized, it is preferable to use the above level to prevent the scattering of the fine particles.\|[0100] In the space, the contact between the rock particles and the air is not particularly restricted, but for example, a tray or the like placed in the space may be placed in a container with a shallow bottom such as a tray having an arbitrary area, and spread in a laminar state over the entire bottom surface of the tray.\|[0101] When stratification of rock particles in this way, it is necessary to consider the diffusion of CO2 into the deepest part of the layer. When rocks are crushed to the micrometer level, the diffusion of carbon dioxide in the air spaces between the particles is considered to be due to molecular diffusion. Therefore, there is a concern that the accumulation of fine rock particles in a thick layer decreases the concentration of carbon dioxide at the lower part (deep part) of the fine rock particles and slows the mineralization reaction. On the other hand, the degree of this deep region depends on the type of rock (compound), the size of the space, the particle size of the fine particles, the flow velocity of the air, etc.\|[0102] Based on the above, the thickness of the rock fine particles (fine particle layer) when spread in a layered state is, for example, preferably 5 cm (50 mm) or less, preferably 1-50 mm, more preferably 1-20 mm, more preferably 1-10 mm, and more preferably 1-5 mm.\|[0103] When the fine particles are put in the tray or the like and brought into contact with the air in the state of spreading the tray or the like in a layered state, the tray or the like may be mounted in a multistage in the height direction in the space.\|[0104] The contact time (reaction time) of air and rock particles. However, as a guide, it can be arbitrarily selected as 7 days to 1 year, for example, between 7 days and 2 months. Depending on the amount and type of rocks, the mineralization reaction is considered to have been completed approximately one year after the contact (mineralization reaction) began.\|[0105] When carbonates are formed in the fine particles of rock and carbon dioxide is mineralized, carbonates are accumulated on the surface of the rock, and the mass of fine particles of rock in which a large number of fine particles are assembled is first heated at less than 100°C to remove the adsorbed water. This procedure and the analytical procedures described below are not necessary if the generated carbonate, etc. are not analyzed.\|[0106] After the water is removed, the amount of mineralized carbon dioxide can be confirmed by comparing the mass change with the mass of the fine particles of the rock before the carbonate formation process as an analytical operation. In addition, carbon dioxide mineralized by thermogravimetric differential thermal analysis (TG-DTA) and X-ray fluorescence analysis (XRF) can be analyzed in detail such as the amount of carbon dioxide (carbonate).\|[0107] In addition, environmentally-harmless carbonates (mainly calcium and magnesium carbonate such as calcium carbonate (CaCO3 and MgCO3). The mineralized rocks can be used, for example, as subbase materials or construction materials for landfill. Thus, the mineralized rocks are environmentally friendly.\|[0108] (C) Effect of the present invention: The present invention is such that carbon dioxide in the air is mineralized as a carbonate by micronizing rocks containing alkaline earth metals and bringing the obtained microparticles into contact with air in a space having a predetermined environment, thereby fixing carbon dioxide to the rocks and removing carbon dioxide in the air.\|[0109] Consequently, the present invention can easily remove carbon dioxide from the air at low cost without using a chemical or using a large-scale facility, etc., and can substantially reduce carbon dioxide because the amount of carbon dioxide generated is small. In addition, there is no need of storing carbon dioxide, and there is no risk in such storage, and the immobilized carbon dioxide becomes a carbonate harmless to the environment, and can be reused together with rocks, so that it is also environmentally friendly.\|[0110] According to the present invention, CDR. can be performed without relying on other technologies and infrastructure. Conventional technologies require a large amount of energy to remove carbon dioxide from the air, and considering the carbon dioxide generated by such energy, many of the technologies have not reduced carbon dioxide substantially. On the other hand, the present invention removes carbon dioxide from the air by a simple method, i.e., a step for atomizing rocks and a step for forming a carbonate by reacting the obtained rock particulates with carbon dioxide in the air. Therefore, the present invention is considered to be a technology that requires less energy and leads to a substantial reduction in carbon dioxide.\|[0111] There are currently two main types of CDRs. These are Bioenergy with Carbon Capture and Storage (BECCS) with carbon dioxide (CO2) recovery and storage, and direct air recovery with carbon dioxide storage (DIRECT Air CO2 Capture with Storage:DACCS).\|[0112] Of these, BECCS relies on biomass combustion, carbon dioxide capture, transport to storage sites, and underground storage. The DACCS also uses machinery to filter carbon dioxide from the air before transport and underground storage. The main points to compare are energy requirements (GJ/t-CO2), land requirements (km2/Mt-CO2), water requirements (m3/t-CO2), the time required for CO2 recovery, biological restrictions (Gt-CO2/year), and cost. In all of these cases, t-CO2 means net carbon dioxide (CO2) removed from the environment (accounting for carbon dioxide emissions from processes and supply chains). ). Table 3 shows the comparison of the present invention and these two technologies. Table 3 confirms that the present invention works more advantageously than other technologies.\|TABLE 3\|[0113] \|[0114] In addition, there are scale-up and scale-out ratio issues. BECCS and DACCS usually limit their use to very large (>1Mt-CO2/year) reservoirs because they require reservoirs and transport infrastructure, and development of reservoirs is costly. On the other hand, the present invention can be applied at any scale, whether in the kg scale or in the Mt scale. Therefore, it is considered that small, medium and large-scale systems can be developed without worrying about transportation, storage, etc.\|[0115] In addition, it is not possible to accurately quantify the amount of CO2 removed by other methods using soil and oceans, and there is also the problem that such other methods may lose future CO2 expected due to the impact of climate change. Since carbon dioxide is immobilized as a carbonate by the above simple means and removed from the air, these problems can also be solved.\|[0116] (D) Variations of embodiments: The embodiments described above represent one aspect of the present invention, and the present invention is not limited to the aforementioned embodiments. Needless to say, the content of the present invention includes variations and improvements provided in the configuration of the present invention and to the extent that the purpose and effects can be achieved. The specific structure, shape, etc. in implementing the present invention are acceptable as other structures, shapes, etc., to the extent that the purpose and effect of the present invention can be achieved. The present invention is not limited to each of the embodiments described above, and any deformation or improvement within the scope of achieving the purpose of the present invention is included in the present invention.\|[0117] For example, although necessary operations for (A) the micronization step and (B) the carbonate formation step are partially illustrated, there is no problem with using other procedures not illustrated, to the extent that they do not interfere with the purpose and effect of the present invention. Similarly, a compound capable of constituting a rock is listed as an example, but since it is only an example, there is no problem in including other compounds in the rock used in the present invention, such as a compound containing an alkaline earth metal. Other specific structures, shapes, etc., in the implementation of the present invention may be other structures, etc., to the extent that the purpose of the present invention can be achieved.\|EMBODIMENTS EXAMPLE\|[0118] The present invention is described in more detail below based on examples, etc., but the present invention is not limited to these.\|[0119] (Reference Example 1, Examples 2 to 6, Reference Example 7, Example 8) The composition shown in Table 4 below (Analytical Means of Compound Composition, etc. are described below as equivalent to rock. 8 types of slag (Example 1 to Example 8 (Example 1, Example 2 to Example 6, Example 7, and Example 8) (Prepared). In addition, "%" indicates the content (mass%) to the whole.\|[0120] (Composition of Slag)\|TABLE 4\|[0121] Slag 1 to slag 8 were ground using a mortar and a scraper, and the ground slag was classified using a sieve. The particle size distribution of the slag particles after classification was measured using an optical microscope equipped with a computer vision operated by "ImageJ" software, which is one of the image processing techniques, and a particle sample with a particle size of 25-90 μm and a particle sample with a particle size of less than 25 μm were obtained respectively. In addition, the elemental compositions of slag (1-8) and the compound compositions of slag (1-8) were analyzed by XRF and Q-XRD, respectively (the compound compositions, etc. are shown in Table 4. ).\|[0122] The obtained fine particle samples were placed in a circular tray of 10cm diameter x 1 cm height respectively, and spread so that the thickness becomes 3 mm.\|[0123] The indoor space of a 22L-volume incubator (3-6815-01 CO2 incubator: made by Azwan Co., Ltd.) was set to have a relative humidity of 90% and a temperature of 30°C. Under such a humidity and temperature, a tray containing a particulate sample is placed in the indoor space of the incubator, the door is closed and sealed, and then air having a carbon dioxide concentration of 5% (slag 1-slag 5) and air having a carbon dioxide concentration of 20% (slag 5-slag 8) are introduced. Air was brought into contact with the particulate samples to mineralize carbon dioxide (form carbonate) so as to maintain this state. The test was performed on 1, 3, 7, 14, 21, and 28 days after the start of study treatment. ). Each sample was tested 3 times (n = 3) (Table 5 shows the mean values. ).\|[0124] After the number of days had elapsed, the particulate samples were measured in mass and carbon dioxide (carbonate) mineralized by thermogravimetric differential thermal analysis (TG-DTA) and X-ray fluorescence analysis (XRF) were analyzed. Table 5 and Table 6 show the mineralization ratio (%) of carbon dioxide corresponding to the number of days elapsed (the experimental value is Table 5, but the predicted value is listed in Table 6 as a reference. ). Two carbon dioxide concentrations were evaluated to confirm the unreacted nuclear model.\|TABLE 5\|[0125] \|TABLE 6\|[0126] \|[0127] From the results of Table 5, firstly, the mineralization ratio of slag 1 and slag 7 is very low (for example, 1% or less under the conducted carbon dioxide concentration conditions (slag 1 is 28 days old, slag 7 is 7 days old). ) can be confirmed. The reason for this is that both slag 1 and slag 7 are originally amorphous phases (amorphous parts). The same applies hereinafter. It is considered that the slag 1 and the slag 7 contain 34.1% and 100%, respectively. Since all (100%) of the slag 7 is an amorphous phase, the mineralization ratio is considered to be low.\|[0128] In the case of the slag (1), on the other hand, the amorphous phase accounts for 34.1% of the total amount, but the amorphous phase still accounts for a high percentage of the total amount. Therefore, crystals are trapped in the amorphous phase, and the crystals are not connected to each other, and only the crystals on the surface react, and therefore the mineralization ratio is considered to be low.\|[0129] Generally, when molten rock (natural rock or slag) is cooled, crystalline or amorphous compounds are formed, but rapid cooling tends to produce amorphous compounds, and slow cooling tends to produce crystals. The distribution of nucleation crystals in molten rock is random, and these crystals grow until they come into contact with other crystals. On the other hand, in the liquid phase between the crystals, if the crystals have solidified as an amorphous phase before growing together, the crystals are separated from each other and cannot be connected. Such an arrangement would hinder the progress of the mineralization of carbon dioxide.\|[0130] In addition, slag 1 and slags other than slag 7 (slags 2 to 6, slags 8) also contained an appropriate amount of amorphous phase. The above behavior was not observed, and the results in Table 5 confirmed that mineralization also progressed well (for example, mineralization rate is 5% or more when the number of days elapsed is 7 under the conducted carbon dioxide concentration conditions. ). This is probably because the amorphous phase occupied the space between the crystalline minerals but did not completely envelop the crystals.\|[0131] The slag (slag 2, slag 4, slag 6, and slag 8) containing a compound such as calcium oxide (oxide) belonging to the group 1 shows mineralization of carbon dioxide at an initial stage. In particular, the rapid mineralization of slag 2 and slag 4 is characterized by the calcium content mainly in oxide form (CaO and Ca2Fe2O5) and calcium silicate (both belong to Group 1). It is considered to be caused by the above.\|[0132] On the other hand, the mineralization ratio of the slag 3 and the slag 5 is relatively lower than that of the slag 3 and the slag 5, because the mixed cation silicate belonging to the group 2 is substituted with Mg or Fe to some extent. It is also considered that there are compounds belonging to Group 4.\|INDUSTRIAL APPLICABILITY\|[0133] The present invention can be advantageously used as a means for providing a technique that enables carbon dioxide in the air to be immobilized as a carbonate on a rock to reduce carbon dioxide in the air, and has high industrial applicability.	(JP7699796)\|TECHNICAL FIELD\|[0001] The present invention relates to a method for removing carbon dioxide from air. More specifically disclosed is a method for removing carbon dioxide from the air, which enables the conversion of carbon dioxide from the air into a useful and harmless state by mineralizing carbon dioxide as a carbonate.\|BACKGROUND ART\|[0002] It is obvious that carbon dioxide emitted into the atmosphere is the cause of global warming, which has been a problem in recent years. Reducing such carbon dioxide emissions is a major challenge in protecting the global environment.\|[0003] Carbon dioxide is naturally captured from the atmosphere through biological processes such as photosynthesis by plant life on land and in the ocean, but the concentration of carbon dioxide in the atmosphere continues to rise. Carbon dioxide is also said to be a factor in the acidification of the world's oceans, which poses a threat to marine ecosystems. On the other hand, systems for fixing and removing exhaust fumes from factories and carbon dioxide (CO2) gas in the atmosphere have been proposed in various ways (for example, see Patent Document 1, etc.). ).\|[0004] Net reduction of global carbon dioxide (CO2) concentrations to eliminate or reduce atmospheric CO2 is It is referred to as NET (Negative Emission Technology) or Carbon Dioxide Removal (CDR.) and various technologies are available (see, for example, Non-Patent Document 1 or Non-Patent Document 3). ).\|[0005] The carbon dioxide emitted must be removed from the atmosphere to stabilize the Earth's climate within a range compatible with modern civilization. Also, in general, the techniques described in the literature described above should be applied to biological systems (e.g., retention of carbon dioxide in soil, plants, or the ocean). ) or highly industrialized machinery that filters carbon dioxide from the air, liquefies it, and stores it underground. And, there was a tendency that chemicals, high temperature and special reactor were required for industrial process which depended on such machinery.\|CITATION LIST\|PATENT LITERATURE\|[0006] Special Report No. 2013-504424\|NON PATENT LITERATURE\|[0007] Nduagu, E., Bergerson, J. and Zevenhoven, R., 2012. Life cycle assessment of CO2 sequestration in magnesium silicate rock A comparative study. Energy Conversion and Management, 55, pp.116-126.\|Ncongwane, M.s., Broadhurst, J.L. and Petersen, J., 2018. Assessment of the potential carbon footprint of engineered processes fwor the mineral carbonation of PGM tailings. International Journal of Greenhouse Gas Control, 77, pp.70-81.\|Keller, d.P., Lenton, A., Littleton, E.w., Oschlies, A., Scott, v. and Vaughan, N.E., 2018. The effects of carbon dioxide removal on the carbon cycle. Current climate change reports, 4(3), pp.250-265.\|DISCLOSURE\|TECHNICAL PROBLEM\|[0008] Carbon dioxide mineralization in rocks occurs naturally over hundreds of thousands of years. However, conventional methods to promote the reaction are high temperature and high pressure, or by adding chemicals. On the other hand, such a method does not reduce greenhouse gases because it has a large energy load and a large amount of carbon dioxide emissions.\|[0009] Concretely, the technology disclosed in the non-patent document 1 has a problem that the substantial reduction in carbon dioxide amount is reduced because carbon dioxide is reacted with carbon dioxide under high temperature and high pressure conditions. In addition, the technology disclosed in Non-Patent Document 2 requires the addition of chemicals and background emissions during its production (e.g., carbon dioxide emissions related to the creation, transportation, termination and disposal of chemicals and additives). As with the technology disclosed in Non-Patent Document 1, substantial CO2 reductions were reduced by the use of CO2-P-P (Carbon Dioxide Reduction Method).\|[0010] Furthermore, the method disclosed in the non-patent document 3 is a method for simply dispersing crushed rocks on the soil surface, which is undesirable because it is difficult to estimate the amount of carbon dioxide mineralization and may adversely affect the environment.\|[0011] The direct removal of carbon dioxide from the atmosphere is only a part of the total amount of carbon dioxide removal (CDR.) that has already been released, which is in line with the climate change reduction target. The removed carbon dioxide must be transported to the appropriate location for disposal and stored deep underground in certain geological structures. These transport and storage systems are too large and costly for individual companies to manufacture and operate, and there are various political, economic, and social risks associated with achieving CDR. dependent on systems that store carbon dioxide underground.\|[0012] The present invention provides an environmentally friendly method for removing carbon dioxide from the air, the method being implemented at a low cost, being capable of substantially reducing carbon dioxide, and being free from the risk of carbon dioxide retention.\|TECHNICAL SOLUTION\|[0013] The method for removing carbon dioxide from the air according to the present invention is a method for removing carbon dioxide from the air, wherein a compound (excluding a carbonate) contains at least one of Ca (calcium) and Mg (magnesium). of rock to obtain fine particles of the rock; and The method includes a carbonate formation step in which the fine particles of the rock thus obtained are brought into contact with air in a space having a temperature of 15-50°C and a relative humidity of 50-100%, and carbonates are formed in the fine particles of the rock The amorphous portion of the rock is 30 mass% or less of the whole, and the fine particles of the rock have a particle diameter of 1-100 μm The fine particles of the rock are put in the tray in a state of spreading in a laminar state over the entire bottom surface of the tray. The rock is characterized in that the rock particles which are brought into contact with the air by placing the tray in the space and spread in the layer form have a thickness of 1 to 50 mm.\|[0014] The method for removing carbon dioxide from the air is characterized in that the rock contains at least one compound from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|[0015] The method for removing carbon dioxide from the air is characterized in that the rock contains, in a total amount, 5 mass% or more of at least one compound from the group consisting of calcium oxide, magnesium oxide, calcium/iron oxide, calcium aluminate and calcium silicate.\|[0017] The method for removing carbon dioxide from the air is characterized in that the rock contains at least one member selected from among ultra-basic rock, basic rock, slag and waste concrete.\|ADVANTAGEOUS EFFECTS\|[0020] The present invention secures carbon dioxide to a rock and removes carbon dioxide from the air by atomizing the rock containing an alkaline earth metal, bringing the obtained particulates into contact with air in a space having a predetermined environment, and mineralizing carbon dioxide in the air as a carbonate.\|[0021] Consequently, the present invention can easily remove carbon dioxide from the air at low cost without using a chemical or using a large-scale facility, etc., and can substantially reduce carbon dioxide because the amount of carbon dioxide generated is small. In addition, there is no need of storing carbon dioxide, and there is no risk in such storage, and the immobilized carbon dioxide becomes a carbonate harmless to the environment, and can be reused together with rocks, so that it is also environmentally friendly.\|DESCRIPTION OF DRAWINGS\|[0022] This chart (Graph 1) shows the change in the mineralization effect (mineralization rate (%)) of carbon dioxide in the atmosphere as a result of measuring the number of elapsed days as 14 days.\| This chart (Graph 2) shows the change in the mineralization effect (mineralization rate (%)) of carbon dioxide in the atmosphere as the number of months in December (one year).\|DESCRIPTION OF EMBODIMENTS\|[0023] An aspect of the present invention is explained below. The method for removing carbon dioxide from the air according to the present invention comprises atomizing a rock containing an alkaline earth metal ((I) atomization step) and bringing the atomized rock into contact with the air in a space having a specific environment Carbon dioxide in the air is mineralized and fixed by using carbon dioxide in the air as a carbonate ((II) carbonate formation process) to remove the carbon dioxide from the air.\|[0024] Step (A): In the step of atomizing, the rock is pulverized to obtain fine particles.\|[0025] (A-1) About rocks: First, I will explain available rocks. Any of natural and man-made rocks can be used as rocks if they are formed from the compounds, etc. shown below. In the present invention, the term "compound" also includes "mineral".\|[0026] Usable rocks are, for example, 0-100°C temperature, suitable moisture (for example, relative humidity of reaction environment is 50-100%, etc.). It is required that the formation of carbonate by reaction with gas phase carbon dioxide under atmospheric pressure is thermodynamically possible. The term "thermodynamically" is taken to mean that 0-dimensional calculation conditions are considered and meso-scale structures are not considered.\|[0027] The rocks usable in the present invention are so-called slags (steel slags, iron slag, etc.), which are composed of a substance containing a mineral component of an ore matrix, etc., which has been separated by melting from a metal to be metallurgically measured, when smelting the metal from the ore, etc., as rocks containing a compound containing an alkaline earth metal. In addition, concrete that was originally used for buildings, etc., such as demolished concrete that is created when the building itself is no longer necessary or when the building, etc. that used the building, etc. is demolished, and surplus concrete itself that occurs when the building, etc. is built, etc. It includes waste concrete (concrete waste) which is concrete, etc., expected to be disposed of in the future, and it is preferable to use these slag and waste concrete. Since the carbonate does not react with carbon dioxide in the air to further become a carbonate, it is excluded from compounds containing alkaline earth metals.\|[0028] The rock contains a compound containing an alkaline earth metal. That is, compounds such as Ca (calcium), Mg (magnesium), Be (beryllium), Sr (strontium), Ba (barium), and Ra (radium), which are alkaline earth metals, are cited, but it is preferable to use a compound of Ca (calcium) and Mg (magnesium), which is largely contained in natural rocks.\|[0029] The following is an example of a compound containing an alkaline earth metal. First, an oxide of a single alkaline earth metal is cited. For example, calcium oxide (CaO) which is an oxide of calcium, magnesium oxide (MgO) which is an oxide of magnesium, and the like can be used.\|[0030] Although barium oxide (BaO), which is an oxide of barium, strontium oxide (SrO), etc., which is an oxide of strontium, etc., it is preferable to use calcium oxide (CaO), magnesium oxide (MgO), which is an oxide of magnesium, etc.\|[0031] Other oxides include magnesium/iron oxides (MgFe2O4, etc.), calcium/iron oxides (Ca2Fe2O5, etc.), magnesium aluminate (magnesium alumina oxide) (MgAl2O4, etc.), calcium aluminate, and calcium oxide. An oxide such as calcium ferroaluminate can be used. For example, calcium aluminate such as Ca3Al2O6, Ca12Al14O33 or calcium iron aluminate such as Ca4Al2Fe2O10 can be used.\|[0032] As the compound, for example, calcium silicate can be used. For example, a calcium silicate such as Ca2SiO4, Ca3Si2O7, Ca3SiO5, CaSiO3 can be transferred.\|[0033] As the compound, for example, magnesium silicate or magnesium aluminosilicate can be used. For example, magnesium silicate such as MgSiO3 and Mg2SiO4 or magnesium aluminosilicate such as Mg3Al2Si3O12 can be used.\|[0034] As the compound, for example, calcium silicate magnesium can be used. For example, a calcium silicate magnesium such as CaMgSiO4, Ca3MgSi2O8, Ca7MgSi4O16, CaMgSi2O6, Ca2MgSi2O7, etc., can be used.\|[0035] As the compound, for example, calcium aluminosilicate can be used. For example, calcium aluminosilicate such as CaAl2Si2O8, Ca2Al2SiO7, Ca3Al2Si3 O12, etc., can be used.\|[0036] As the compound, for example, calcium silicate iron can be used. For example, CaFeSiO4, (Ca/Fe)SiO3, (Ca/Fe)2SiO4, Ca3Fe2Si3O12, CaFeSi2O6, Ca0.82Fe0.18SiO2, etc., Ca(Fe/Mg)Si2O6, Calcium iron silicate, calcium magnesium iron silicate, magnesium iron silicate, etc. can be used.\|[0037] For example, calcium silicate iron can be CaXFe2-XSiO4 (0<X<2). A compound obtained by substituting iron for the calcium silicate magnesium moiety or a compound obtained by substituting magnesium for the iron moiety of the calcium silicate iron may also be used.\|[0038] In the application of the present invention to a compound containing an alkaline earth metal, including the above-described compound, the reactivity of the original compound (i.e., difficulty in mineralizing carbon dioxide due to contact with carbon dioxide or difficulty in mineralizing carbon dioxide. This suggests that there is a difference in the reactivity when pulverized and atomized.\|[0039] Figures 1 and 2 show that the compounds listed in Figures 1 and 2 are selected from the above compounds, and pulverized so that their particle sizes are less than 3 μm. Assuming the temperature is 30°C and the relative humidity is 90%, the change in the mineralization effect (mineralization ratio (%)) of carbon dioxide (carbon dioxide concentration: 415ppm) in the atmosphere for the target compound is estimated to be 14 days old (the compound shown in Figure 1). The figure shows the results when the number of months elapsed is measured as December (one year) (the compound listed in Figure 2). Fig. 1 is referred to as "graph 1" and Fig. 2 is referred to as "graph 2".\|[0040] The mineralization ratio (%) is the actual mineralization amount of each compound relative to the CO2 (carbon dioxide) mineralization amount potential represented by formula (I) (see formula (II)). ).\|[0041] The CO2 mineralization potential indicates the amount of mineralization that is ideally achievable, and the mineralization rate (%), which is the ratio of the actual amount of mineralization to the potential, is an index indicating the degree of ease of mineralization (mineralization reaction).\|[0042] \|[0043] \|[0044] From Figures 1 and 2, the compounds listed in Figure 1 (CaO, MgO, Ca2SiO4, CaSiO3) have excellent reactivity and are shown to be highly reactive. (In Fig. 2, the lines of Mg2SiO4 and MgSiO3 results almost overlap. ). In addition to Figures 1 and 2, Table 1 shows that the CO2 mineralization potential (kg-CO2/kg) is determined by selecting the compounds listed in Table 1 from the above compounds. If the particle size of the crushed compound is 1 to 3 μm, the mineralization rate (%) after 1 year when it is 5 to 10 μm (Table 1 abbreviates "mineralization rate", but it is agreed with the mineralization rate (the same as the others). ) is shown.\|TABLE 1\|[0045] \|[0046] Although the above compound (mineral) is an example, it can be confirmed that the mineralization ratio of calcium oxide (CaO), magnesium oxide (MgO), calcium/iron oxide, calcium aluminate, and calcium silicate, which are oxides of alkaline earth metals, is high.\|[0047] From this result, it is preferable that the rocks used in the present invention contain these compounds, which are referred to as "Group 1" in Table 1 (corresponding to "Group 1" described below). ).\|[0048] 1, 2, and Table 1 indicate that these compounds have high mineralization rates (fast mineralization reaction) and, when contained in rocks, can form carbonates efficiently by contact with carbon dioxide in the air.\|[0049] According to the results of Table 1, etc., the compounds can be divided into the following groups 1 to 3. Each group is considered to have the following characteristics regarding mineralization.\|[0050] In addition, natural rocks, slag, waste concrete, etc., often contain compounds other than the above compounds, i.e., compounds not containing alkaline earth metals. For example, silicon oxide (SiO2), aluminum oxide (alumina) (Al2O3), aluminosilicate, iron oxide (FeO, Fe2O3, Fe3O4), and aluminum oxide are oxides. Compounds (minerals) such as manganese oxide (MnO), iron silicate (FeSiO3, Fe2SiO4), carbonate, and alkali minerals are enumerated. All of these are pulsate stones, which are essentially unnecessary compounds (ores).\|[0051] Compounds such as these compounds that do not contain alkaline earth metals, such as calcium and magnesium, do not form carbonates even when ground and brought into contact with carbon dioxide under prescribed conditions (Group 4). ). The group 4 also contains a compound which cannot form a carbonate under a predetermined condition.\|[0052] Based on the results of Table 1 and other data, Groups 1 through 4 are defined as follows by the degree of mineralization reaction.\|[0053] Group 1: Carbon dioxide mineralization is roughly completed (>95%) within 1 year if the particle size is crushed to 1 to 3 μm. When the particle size is crushed to 5 to 10 μm, it is 60% or more. Refers to compounds (minerals) that are considered possible (highly reactive compounds). For example, calcium oxide (CaO), Magnesium oxide (MgO), oxide of calcium/iron oxide (Ca2Fe2O5, etc.), Ca3Al2O6, Ca12. The composition contains at least one compound among calcium aluminate such as Al14O33 and calcium silicate such as Ca2SiO4, Ca3Si2O7, Ca3SiO5, and CaSiO3 The compounds, etc. listed in Group 1 in Table 1 are enumerated. Further, the compounds containing an alkaline earth metal, as described in the present invention, such as these compounds and the compounds of the second group, include compounds that are partially substituted with other elements and that are construed to belong to these compounds. Concretely, a compound such as calcium silicate, magnesium silicate or calcium magnesium silicate wherein a part of calcium ion or magnesium ion is replaced by iron ion may be used.\|[0054] Group 2: Compounds that, even when milled to 1 to 3 μm in particle size, are considered to have a carbon dioxide mineralization rate of 10 to 95% within 1 year (compounds with normal reactivity). For example, calcium ferrous aluminate such as Ca4Al2Fe2O10, magnesium silicate such as MgSiO3 and Mg2SiO4, calcium aluminosilicate such as CaMgSiO4, Ca3MgSi2O8, Ca2MgSi2O7, Ca7MgSi4O16, CaMgSi2O6, calcium silicate magnesium silicate such as Ca2Al2SiO7, CaAl2Si2O8, etc., and MgAl2O4. The term "A-" refers to amorphous (amorphous) compounds such as oxide (magnesium aluminate), magnesium/iron oxide such as MgFe2O4, A-CaMgSiO4, A-Ca2MgSi2O7, A-Ca3Si2O7, and A-CaSiO3. The same applies hereinafter. Table 1, Group 2 (2). Compounds listed in the table above are examples.\|[0055] Group 3: Refers to compounds (compounds with slightly lower reactivity) that are considered to have a carbon dioxide mineralization rate of less than 10% within 1 year, even if the particle size is crushed to 1 to 3 μm. For example, Group 3 (3 in Table 1 includes A-Ca3SiO5, A-CaAl2Si2O8, A-Ca2SiO4, A-MgSiO3, A-Ca2Al2SiO7, A-Ca3MgSi2O8, A-Ca7MgSi4O16, A-Ca2Fe2O5, A-CaMgSi2O6, etc. Compounds listed in the table above are examples.\|[0056] Group 4: Alkaline earth metals (calcium, magnesium, etc.) It is a compound that does not contain carbonic acid (including thrombophiles), or that is thought to be unable to form carbonic acid under ambient conditions. (Chemical compounds that cannot be expected to react). For example, silicon oxide (SiO2), aluminum oxide (alumina) (Al2O3), iron oxide (FeO, Fe3O4, Fe2O5, etc. Examples include manganese oxide (MnO), iron silicate (FeSiO3, Fe2SiO4), carbonate, and alkaline minerals.\|[0057] As the rocks to be applied to the method of the present invention, the ratio of the groups 1 to 4 is considered to be important. In the above group, the reactivity is highest when the group 1 is considered as a single compound and lowest when the group 4 is considered as a single compound (reactivity is Group 1>Group 2>Group 3>Group 4. ).\|[0058] It goes without saying that the composition of the rocks used is better if they have a high content of compounds belonging to the group with high reactivity. The range of the content of each group is shown below, but as described below, reactivity includes the presence of other components of the rock (natural rocks include the presence of pulsels, etc.). Therefore, the following range is only one criterion, because it depends on the particle size (particle size) obtained in the particle processing, the carbon dioxide concentration of the air in contact, etc.\|[0059] I would like to expect that the compounds belonging to Group 1 are present as much as possible in rocks compared with the compounds of other groups, but in the case of natural rocks, there are many cases where it is not known unless it is mined, so it cannot be determined uniformly.\|[0060] In consideration of such circumstances, the following compounds belong to Group 1: (i) Calcium oxide, Magnesium oxide, Calcium/Iron oxide, Calcium aluminate, Calcium silicate, etc. The rock preferably contains not less than 5% by mass relative to the whole rock, more preferably not less than 10% by mass, and particularly not less than 15% by mass. The more compounds in Group 1, such as all of the rocks (100% by mass) or more than 90% by mass of the whole rock, the better the mineralization performance of the rock. The content which can actually be expected is limited to about 25 mass%, and it is considered that 5 to 20 mass% should be contained. In addition, the compounds belonging to Group 1 are generally contained in an amount of 5 to 20 mass% relative to the total amount of the natural rocks when the compounds of Group 1 are present. In the case of slag, waste concrete, etc., the content is often 0 to 90 mass%.\|[0061] Compounds belonging to Group 2 (excluding those amorphized in Table 1) In the case of a rock containing a compound belonging to Group 1, it is preferable to contain as much of the remainder (generally 80-100 mass% of the remainder) excluding the compound belonging to Group 1 as possible, because the rock does not want to contain the compound belonging to Group 3 and Group 4 described below as much as possible.\|[0062] On the other hand, when not containing a compound belonging to Group 1, the compound belonging to Group 2 is preferably contained in an amount of 50 mass% or more, preferably in an amount of 70 mass% or more, and particularly preferably in an amount of 70-100 mass%, with respect to the whole rock. In the case of natural rocks, the amount of compounds belonging to Group 2 is approximately 70-100% by mass in total relative to the whole rock (in the case of no compounds belonging to Group 1, the amount of total compounds belonging to Group 1 is about 70-100% by mass in the case of natural rocks. When present, it is generally contained in an amount of 0 to 25 mass%. When used in slag, waste concrete, etc., it is often contained in an amount of 0 to 30 mass%.\|[0063] It is preferable that the compounds belonging to Group 3, Group 4 are not present as much as possible.\|[0064] When the rock is a natural rock, for example, magnesium oxide (MgO), calcium oxide (CaO), magnesium silicate, calcium silicate magnesium, and magnesium iron silicate can be mainly used in the present invention.\|[0065] Natural rocks, for example, igneous rocks, sedimentary rocks, metamorphic rocks, etc., are considered, but igneous rocks are preferably used. Although the igneous rock may be a deep rock, volcanic rock, etc., it is preferable to use the deep rock.\|[0066] From the content of SiO2, the rock is acidic (generally, the content of SiO2 exceeds 66 mass% of the whole). The SiO2 content is 52-66% by mass. Rock mass: 45-52% by mass (basic rock), 45-52% by mass (suprabasic rock), 45% by mass or less (basic rock). ) can be listed. In the present invention, it is preferable to use a suprabasic rock or a basic rock, and particularly preferable to use a suprabasic rock.\|[0067] Suprabasic rocks, also called suprapaceous rocks, are generally composed of ornithospherite, dang ornithospherite, serpentine, ornithospherite ornithospherite, monolithospherite ornithospherite, bibiornithospherite ornithospherite, komatiite, etc. Basic rocks are also called mafic rocks, and generally consist of mottled rocks, basaltic rocks, drylights, etc.\|[0068] The basic rock is composed mainly of magnesium silicate (magnesium silicate) and CaSi such as MgSiO3 (olivine) and Mg2SiO4 (olivine). Contains mgSi2O6 (pyroxite), and may also contain a silicated mineral such as CaAl2Si2O8. The magnesium silicate belongs to the group 2, and the mineralization reaction is not so fast.\|[0069] On the other hand, magnesium oxide (MgO) belonging to Group 1 and very fast mineralization reaction (generally considered to be about 0 to 10 mass% in general, but it is not limited to this range) is appropriate for the ultra-basic rock. It is considered that the total amount of the compounds in Group 1 is about 5 to 20 mass%. In addition, it is a natural rock suitable for mineralization because silica (SiO2) and alumina silicate are hardly contained in the suprabasic rock. In addition, ultrafine rocks are natural rocks that are widely available in large quantities.\|[0070] The basic rock is composed mainly of CaAl2Si2O8 and other suitable compounds. and CaMgSi2O6 (pyroxene). Magnesium silicate (magnesium silicate) such as MgSiO3 (talc), Mg2SiO4 (talc), etc. are also included.\|[0071] Rocks containing many amorphous (amorphous) compounds (rocks with a large amount of amorphous phase) have low reactivity and often interfere with mineralization. Since they envelop other crystals and are involved in the amorphous phase, they are connected to each other (it is important to advance the mineralization reaction). (This will prevent you from doing so.\|[0072] In the state of the rock before grinding, the amorphous portion of the rock (the rock having a large amount of an amorphous phase) containing a large amount of an amorphous compound is generally preferred to be 30 mass% or less. If the proportion of amorphous (amorphous) parts is 30 mass% or less, it is considered that completely enclosing the crystals is suppressed, even if the amorphous phase (amorphous part) may occupy the space between the crystalline minerals. The above range includes the presence of other components of the rock (natural rock includes the presence of pulsatile rocks, etc.). Therefore, the range of exposure depends on the particle size (particle size) and the carbon dioxide concentration of the air in contact with the particles.\|[0073] (A-2) Pulverization: In the case of natural rocks, the rock is mined and then pulverized to form fine particles. In the micronization process, the crystal state of each rock-forming compound is maintained (amorphous). (This is important.\|[0074] When the compound constituting the rock is pulverized into fine particles, the smaller the particle size, the larger the surface area of the fine particles and the larger the contact surface with air (carbon dioxide). However, if the particle size is too small, the rock becomes amorphous and the reactivity to mineralization decreases.\|[0075] Of the above compounds, the compounds listed in Table 2 are selected, and the approximate particle size (amorphous diameter) to be amorphous (amorphous diameter) when pulverized into fine particles is listed in Table 2. In addition, "grinding efficiency of each compound" and "effective rate of mineralization" are also listed in Table 2. In addition, the amorphization diameter shown in Table 2 is only a guide, and it does not reliably amorphize if it is below this diameter.\|TABLE 2\|[0076] \|[0077] The time t required for the reaction of the fine particles having a radius of R(m) to reach the depth δ is expressed in formula (III). The concentration of calcium (Ca) and magnesium (Mg) in a solid is ρ, the vapor phase concentration of CO2 is Cg, and the diffusion coefficient of ions through the product layer is D (m2/s).\|[0078] \|[0079] t: Time (sec) ρ: Sum of molar density of magnesium (Mg) and calcium (Ca) in rock (moles/m3-rock) R: Radius of fine particles (m) D: Concentration of CO in the compound Diffusion coefficient of CO2 (m2/s)Cg: CO2 molar concentration in gas phase (moles/m3-gas) δ: Reaction depth (m)\|[0080] On the other hand, if the radius (particle size) of the fine particles is too large, it takes a very long time for all of the fine particles to react, which is also undesirable. According to the unreacted nuclear model, the reaction rate is considered to be inversely proportional to the cube of the diameter of the particles. For example, if the crushing result is 6 μm as a result of assuming 3 μm, the reaction is considered to be 8 (23) times slower.\|[0081] The diffusion coefficient, D, represents the rate of CO2 diffusion through the product layer in the unreacted nuclear model (m2/s), and does not directly represent the mineralization rate of carbon dioxide because of other factors. Since diffusion through the product layer is a rate-limiting step of pneumonialization of CO2, a large diffusion coefficient D actually indicates a mineral that rapidly mineralizes carbon dioxide.\|[0082] The outer diameter (particle size) of the fine particles is determined by the mass of the compound belonging to the above group 1 relative to the total fine particles of the rock obtained. It is considered that the reaction proceeds without crushing the rock more finely than necessary, and that the generation of carbon dioxide by energy loss or crushing can be suppressed, and in addition, the amorphization of the rock (compound) can be suppressed.\|[0083] On the other hand, the reactivity of the whole rock is determined by the type of other components of the rock (natural rock includes the presence of pulsatile rocks, etc.). The composition of the rock may also be referred to as the "rock element", and the composition and composition of the crystalline layer and the amorphous phase, the relationship between the crystalline layer and the amorphous phase, and other factors such as the amount of carbon dioxide oxidation (hereinafter referred to as the "rock element") may also be used. The range of particle size of the crushed rock is also affected by these factors.\|[0084] In view of these facts, when microparticulating rocks, the particle size of the fine particles is generally preferably 100 μm or less (more preferably 50 μm or less, more preferably 25 μm or less, more preferably 10 μm or less. In consideration of the rock elements, appropriate selection may be made, for example, within the range of particle sizes of 1-25 μm, 1-20 μm, 1-10 μm, 1-5 μm, 1-3 μm, etc. For example, when a first group of highly reactive compounds is contained, the particle size may be 1-25 μm (preferably 1-10 μm).\|[0085] If the particle size is 1 to 3 μm, the surface area is large and good reactivity can be expected, but as shown in Table 2, if the particle size is made too small, amorphization may progress and the reactivity may actually become poor. Therefore, it is preferable to limit the particle size of 1 to 3 μm to about 1 to 10 μm or less with the target of 1 to 3 μm. Regarding the particle size of the fine particles, for example, the fine particles of the crushed rock can be spread so as not to overlap, the image acquired by the optical microscope or the like can be analyzed by a computer, and the particle diameter (particle diameter) and shape of the complete distribution of the fine particles can be determined (preferably, the maximum particle diameter is adopted. ). It is desirable that at least 5000 (or 10000) particles are analyzed for each sample of the compound.\|[0086] The rock crushing operation in the micronization can be performed by using a conventionally known crushing means, but, for example, it is preferable to perform the rock by using vertical roller mill, high pressure grinding rolls, etc. It should be noted that ball mills generally have low energy efficiency and tend to become amorphous.\|[0087] In the case of simply atomizing the rock, the rock may be put into a mortar and crushed by using a mortar and a scraper to obtain a desired particle size. In the crushing of rocks by mortar and mortar, for example, it is possible to achieve a very low degree of amorphization by separating very small fine particles that are expected to have been amorphized when they are produced and carrying out a minimum amount of crushing to achieve a desired particle size.\|[0088] Rock crushing prevents amorphization, reduces particle distribution (size distribution of fine particles) as much as possible, minimizes energy consumption (energy consumption generates carbon dioxide, and substantial carbon dioxide reduction is reduced. (3) should be taken into account. These are considered to be particles that have become too small (amorphous) while grinding, for example, using high-pressure grinding. Also, the load of the crusher can be reduced (energy efficiency can be increased) by separating. (This will be retained for the purpose of separation.) On the other hand, the low-pressure grinding (low-pressure grinding) is preferably ground by a vertical roller mill, which is considered to be an aspect of the high-pressure grinding means, because the supplied energy causes dislocation (amorphization) of the crystal structure and generation of heat and sound (energy loss).\|[0089] It is preferable to reduce (narrow) the particle distribution in rock crushing as much as possible. By narrowing the particle distribution, the air to be contacted to mineralize carbon dioxide diffuses into the particulate layer.\|[0090] Such diffusion is an important factor in CO2 mineralization, and it is considered inefficient that the wide particle distribution reduces the porosity between particles, and only the upper part of the ground layer comes into contact with CO2. Less diffusion means that the rock is spread into a thinner layer (the rock layer becomes thinner. It means that it is necessary. The thinning of the rock layer is undesirable because it reduces the amount of rock that can be processed per unit volume of the equipment and at the same time increases the number of sheets per unit rock, which increases the cost.\|[0091] A commercial air classifier or a sieve, etc., may be used for classification. A pulverizer having a classification function may also be used. The particle size distribution is performed by using a conventional technique (for example, measuring the classified fine particles by using an optical microscope equipped with a computer vision operated by commercial software). (You can use it to do this.\|[0092] For example, as also described in CaMgSiO4 in Table 1, there are cases where the compound that has become amorphous as a result of microparticle formation mineralizes CO2 more rapidly than a compound that is not amorphous (crystalline compound). In this case, since the structure of the amorphous compound changes depending on the ratio of the cation to the silica, certain compositions such as CaMgSiO4 favorably react with carbon dioxide even in the case of an amorphous structure and mineralization proceeds.\|[0093] On the other hand, such cases are an exception, and from the point of view of engineering, you will never find pure minerals, and there is always a certain degree of mixing and variation in composition. Therefore, the significant reduction in carbon dioxide mineralization associated with most amorphous compounds outweighs the small performance gains of some compounds. In other words, it is preferable to avoid amorphous compounds because the reaction rate with carbon dioxide and the rate of mineralization are likely to be very low.\|[0094] Further, it is preferable that the rock fine particles obtained by the micronization step are not present as much as possible in the rock fine particles, because the mineralization reaction cannot be expected for the group 4 (compound not expected to react) originally contained in the rock fine particles due to the amorphization of the rock or the amorphization of the rock fine particles together with the micronization. These are preferably about 80 mass% or less in total, and are particularly preferably 50 mass% or less.\|[0095] (B) Carbonate formation process: Fine particles of the rock obtained are brought into contact with air in a predetermined space, whereby carbonates are formed in the fine particles. In other words, carbon dioxide in the air reacts with the fine particles of the rock composed of the above composition, and carbonates (mainly carbonates such as calcium and magnesium) are formed on the surface of the fine particles or in the inside thereof. As a result, carbon dioxide in the air is removed.\|[0096] The space shall be in a state where air is constantly stable (such as stably supplying air containing carbon dioxide and maintaining the conditions described below for the period of implementation, etc.). However, such a stable state can be easily and reliably formed, and it is preferable to use the stone in the room. The space is preferably a closed space capable of supplying air at a certain frequency by ventilation or the like.\|[0097] The introduced air refers to air in general that contains carbon dioxide, for example, the atmosphere (carbon dioxide content is considered to be about 400 to 450 ppm. All gases that are considered to contain carbon dioxide (CO2), such as exhaust gas, can be used. There are also no restrictions on the CO2 concentration of the air in question.\|[0098] The space is conditioned to have a temperature of 15 to 50°C and a relative humidity of 50 to 100%. Both the temperature condition and the humidity condition are within the aforementioned ranges, so that carbon dioxide is mineralized efficiently. The temperature in the space is preferably 20-40°C, and is particularly preferably 30-35°C. The relative humidity is preferably 60-95%.\|[0099] The flow rate of air containing carbon dioxide in a space can be appropriately determined according to the concentration of carbon dioxide, the type and composition of rocks. For example, a natural suprabasic rock (ultrapascular stone) is used as a rock, and the air to be carbon dioxide removed is used as the atmosphere (the carbon dioxide content is at the same level as described above). In this case, it is preferable that the exposure rate be approximately 1 to 100mm/sec, and particularly preferably 1 to 10mm/sec. Since the fine particles of the rock have a small particle diameter and are pulverized, it is preferable to use the above level to prevent the scattering of the fine particles.\|[0100] In the space, the contact between the rock particles and the air is not particularly restricted, but for example, a tray or the like placed in the space may be placed in a container with a shallow bottom such as a tray having an arbitrary area, and spread in a laminar state over the entire bottom surface of the tray.\|[0101] When stratification of rock particles in this way, it is necessary to consider the diffusion of CO2 into the deepest part of the layer. When rocks are crushed to the micrometer level, the diffusion of carbon dioxide in the air spaces between the particles is considered to be due to molecular diffusion. Therefore, there is a concern that the accumulation of fine rock particles in a thick layer decreases the concentration of carbon dioxide at the lower part (deep part) of the fine rock particles and slows the mineralization reaction. On the other hand, the degree of this deep region depends on the type of rock (compound), the size of the space, the particle size of the fine particles, the flow velocity of the air, etc.\|[0102] Based on the above, the thickness of the rock fine particles (fine particle layer) when spread in a layered state is, for example, preferably 5 cm (50 mm) or less, preferably 1-50 mm, more preferably 1-20 mm, more preferably 1-10 mm, and more preferably 1-5 mm.\|[0103] When the fine particles are put in the tray or the like and brought into contact with the air in the state of spreading the tray or the like in a layered state, the tray or the like may be mounted in a multistage in the height direction in the space.\|[0104] The contact time (reaction time) of air and rock particles. However, as a guide, it can be arbitrarily selected as 7 days to 1 year, for example, between 7 days and 2 months. Depending on the amount and type of rocks, the mineralization reaction is considered to have been completed approximately one year after the contact (mineralization reaction) began.\|[0105] When carbonates are formed in the fine particles of rock and carbon dioxide is mineralized, carbonates are accumulated on the surface of the rock, and the mass of fine particles of rock in which a large number of fine particles are assembled is first heated at less than 100°C to remove the adsorbed water. This procedure and the analytical procedures described below are not necessary if the generated carbonate, etc. are not analyzed.\|[0106] After the water is removed, the amount of mineralized carbon dioxide can be confirmed by comparing the mass change with the mass of the fine particles of the rock before the carbonate formation process as an analytical operation. In addition, carbon dioxide mineralized by thermogravimetric differential thermal analysis (TG-DTA) and X-ray fluorescence analysis (XRF) can be analyzed in detail such as the amount of carbon dioxide (carbonate).\|[0107] In addition, environmentally-harmless carbonates (mainly calcium and magnesium carbonate such as calcium carbonate (CaCO3 and MgCO3). The mineralized rocks can be used, for example, as subbase materials or construction materials for landfill. Thus, the mineralized rocks are environmentally friendly.\|[0108] (C) Effect of the present invention: The present invention is such that carbon dioxide in the air is mineralized as a carbonate by micronizing rocks containing alkaline earth metals and bringing the obtained microparticles into contact with air in a space having a predetermined environment, thereby fixing carbon dioxide to the rocks and removing carbon dioxide in the air.\|[0109] Consequently, the present invention can easily remove carbon dioxide from the air at low cost without using a chemical or using a large-scale facility, etc., and can substantially reduce carbon dioxide because the amount of carbon dioxide generated is small. In addition, there is no need of storing carbon dioxide, and there is no risk in such storage, and the immobilized carbon dioxide becomes a carbonate harmless to the environment, and can be reused together with rocks, so that it is also environmentally friendly.\|[0110] According to the present invention, CDR. can be performed without relying on other technologies and infrastructure. Conventional technologies require a large amount of energy to remove carbon dioxide from the air, and considering the carbon dioxide generated by such energy, many of the technologies have not reduced carbon dioxide substantially. On the other hand, the present invention removes carbon dioxide from the air by a simple method, i.e., a step for atomizing rocks and a step for forming a carbonate by reacting the obtained rock particulates with carbon dioxide in the air. Therefore, the present invention is considered to be a technology that requires less energy and leads to a substantial reduction in carbon dioxide.\|[0111] There are currently two main types of CDRs. These are Bioenergy with Carbon Capture and Storage (BECCS) with carbon dioxide (CO2) recovery and storage, and direct air recovery with carbon dioxide storage (DIRECT Air CO2 Capture with Storage:DACCS).\|[0112] Of these, BECCS relies on biomass combustion, carbon dioxide capture, transport to storage sites, and underground storage. The DACCS also uses machinery to filter carbon dioxide from the air before transport and underground storage. The main points to compare are energy requirements (GJ/t-CO2), land requirements (km2/Mt-CO2), water requirements (m3/t-CO2), the time required for CO2 recovery, biological restrictions (Gt-CO2/year), and cost. In all of these cases, t-CO2 means net carbon dioxide (CO2) removed from the environment (accounting for carbon dioxide emissions from processes and supply chains). ). Table 3 shows the comparison of the present invention and these two technologies. Table 3 confirms that the present invention works more advantageously than other technologies.\|TABLE 3\|[0113] \|[0114] In addition, there are scale-up and scale-out ratio issues. BECCS and DACCS usually limit their use to very large (>1Mt-CO2/year) reservoirs because they require reservoirs and transport infrastructure, and development of reservoirs is costly. On the other hand, the present invention can be applied at any scale, whether in the kg scale or in the Mt scale. Therefore, it is considered that small, medium and large-scale systems can be developed without worrying about transportation, storage, etc.\|[0115] In addition, it is not possible to accurately quantify the amount of CO2 removed by other methods using soil and oceans, and there is also the problem that such other methods may lose future CO2 expected due to the impact of climate change. Since carbon dioxide is immobilized as a carbonate by the above simple means and removed from the air, these problems can also be solved.\|[0116] (D) Variations of embodiments: The embodiments described above represent one aspect of the present invention, and the present invention is not limited to the aforementioned embodiments. Needless to say, the content of the present invention includes variations and improvements provided in the configuration of the present invention and to the extent that the purpose and effects can be achieved. The specific structure, shape, etc. in implementing the present invention are acceptable as other structures, shapes, etc., to the extent that the purpose and effect of the present invention can be achieved. The present invention is not limited to each of the embodiments described above, and any deformation or improvement within the scope of achieving the purpose of the present invention is included in the present invention.\|[0117] For example, although necessary operations for (A) the micronization step and (B) the carbonate formation step are partially illustrated, there is no problem with using other procedures not illustrated, to the extent that they do not interfere with the purpose and effect of the present invention. Similarly, a compound capable of constituting a rock is listed as an example, but since it is only an example, there is no problem in including other compounds in the rock used in the present invention, such as a compound containing an alkaline earth metal. Other specific structures, shapes, etc., in the implementation of the present invention may be other structures, etc., to the extent that the purpose of the present invention can be achieved.\|EMBODIMENTS EXAMPLE\|[0118] The present invention is described in more detail below based on examples, etc., but the present invention is not limited to these.\|[0119] (Reference Example 1, Examples 2 to 6, Reference Example 7, Example 8) The composition shown in Table 4 below (Analytical Means of Compound Composition, etc. are described below as equivalent to rock. 8 types of slag (Example 1 to Example 8 (Example 1, Example 2 to Example 6, Example 7, and Example 8) (Prepared). In addition, "%" indicates the content (mass%) to the whole.\|[0120] (Composition of Slag)\|TABLE 4\|[0121] Slag 1 to slag 8 were ground using a mortar and a scraper, and the ground slag was classified using a sieve. The particle size distribution of the slag particles after classification was measured using an optical microscope equipped with a computer vision operated by "ImageJ" software, which is one of the image processing techniques, and a particle sample with a particle size of 25-90 μm and a particle sample with a particle size of less than 25 μm were obtained respectively. In addition, the elemental compositions of slag (1-8) and the compound compositions of slag (1-8) were analyzed by XRF and Q-XRD, respectively (the compound compositions, etc. are shown in Table 4. ).\|[0122] The obtained fine particle samples were placed in a circular tray of 10cm diameter x 1 cm height respectively, and spread so that the thickness becomes 3 mm.\|[0123] The indoor space of a 22L-volume incubator (3-6815-01 CO2 incubator: made by Azwan Co., Ltd.) was set to have a relative humidity of 90% and a temperature of 30°C. Under such a humidity and temperature, a tray containing a particulate sample is placed in the indoor space of the incubator, the door is closed and sealed, and then air having a carbon dioxide concentration of 5% (slag 1-slag 5) and air having a carbon dioxide concentration of 20% (slag 5-slag 8) are introduced. Air was brought into contact with the particulate samples to mineralize carbon dioxide (form carbonate) so as to maintain this state. The test was performed on 1, 3, 7, 14, 21, and 28 days after the start of study treatment. ). Each sample was tested 3 times (n = 3) (Table 5 shows the mean values. ).\|[0124] After the number of days had elapsed, the particulate samples were measured in mass and carbon dioxide (carbonate) mineralized by thermogravimetric differential thermal analysis (TG-DTA) and X-ray fluorescence analysis (XRF) were analyzed. Table 5 and Table 6 show the mineralization ratio (%) of carbon dioxide corresponding to the number of days elapsed (the experimental value is Table 5, but the predicted value is listed in Table 6 as a reference. ). Two carbon dioxide concentrations were evaluated to confirm the unreacted nuclear model.\|TABLE 5\|[0125] \|TABLE 6\|[0126] \|[0127] From the results of Table 5, firstly, the mineralization ratio of slag 1 and slag 7 is very low (for example, 1% or less under the conducted carbon dioxide concentration conditions (slag 1 is 28 days old, slag 7 is 7 days old). ) can be confirmed. The reason for this is that both slag 1 and slag 7 are originally amorphous phases (amorphous parts). The same applies hereinafter. It is considered that the slag 1 and the slag 7 contain 34.1% and 100%, respectively. Since all (100%) of the slag 7 is an amorphous phase, the mineralization ratio is considered to be low.\|[0128] In the case of the slag (1), on the other hand, the amorphous phase accounts for 34.1% of the total amount, but the amorphous phase still accounts for a high percentage of the total amount. Therefore, crystals are trapped in the amorphous phase, and the crystals are not connected to each other, and only the crystals on the surface react, and therefore the mineralization ratio is considered to be low.\|[0129] Generally, when molten rock (natural rock or slag) is cooled, crystalline or amorphous compounds are formed, but rapid cooling tends to produce amorphous compounds, and slow cooling tends to produce crystals. The distribution of nucleation crystals in molten rock is random, and these crystals grow until they come into contact with other crystals. On the other hand, in the liquid phase between the crystals, if the crystals have solidified as an amorphous phase before growing together, the crystals are separated from each other and cannot be connected. Such an arrangement would hinder the progress of the mineralization of carbon dioxide.\|[0130] In addition, slag 1 and slags other than slag 7 (slags 2 to 6, slags 8) also contained an appropriate amount of amorphous phase. The above behavior was not observed, and the results in Table 5 confirmed that mineralization also progressed well (for example, mineralization rate is 5% or more when the number of days elapsed is 7 under the conducted carbon dioxide concentration conditions. ). This is probably because the amorphous phase occupied the space between the crystalline minerals but did not completely envelop the crystals.\|[0131] The slag (slag 2, slag 4, slag 6, and slag 8) containing a compound such as calcium oxide (oxide) belonging to the group 1 shows mineralization of carbon dioxide at an initial stage. In particular, the rapid mineralization of slag 2 and slag 4 is characterized by the calcium content mainly in oxide form (CaO and Ca2Fe2O5) and calcium silicate (both belong to Group 1). It is considered to be caused by the above.\|[0132] On the other hand, the mineralization ratio of the slag 3 and the slag 5 is relatively lower than that of the slag 3 and the slag 5, because the mixed cation silicate belonging to the group 2 is substituted with Mg or Fe to some extent. It is also considered that there are compounds belonging to Group 4.\|INDUSTRIAL APPLICABILITY\|[0133] The present invention can be advantageously used as a means for providing a technique that enables carbon dioxide in the air to be immobilized as a carbonate on a rock to reduce carbon dioxide in the air, and has high industrial applicability.	Family Number\|(102507569)\|102507569\|Advantages / Prev. Drawbacks\|(JP2022169854 A)\|Accordingly, the present invention enables the easy removal of carbon dioxide from the air at low cost without the use of any chemical or without the use of any large-scale equipment or the like, and also enables the substantial reduction of carbon dioxide because of the reduced amount of carbon dioxide to be (...) \|Moreover, the method disclosed in non-patent document 3 is a method of simply dispersing crushed rock on the soil surface, but it was not preferable because it is difficult to estimate the mineralization amount of carbon dioxide and it can adversely affect the environment.\|	Chemical engineering\|Environmental technology	Y02C-020/40		Y02C-020/40	B01D-053/14\|B01J-020/02\|B01J-020/04\|B01J-020/06\|B01J-020/08\|B01J-020/10	B01D-053/14\|B01J-020/02\|B01J-020/04\|B01J-020/06\|B01J-020/08\|B01J-020/10			WO202604248\|JP2026006164\|JP2025117160	WO202604248 117257809 WHO=Examiner SELF=N CAT=Y\|JP2026006164 117257809 WHO=Applicant SELF=N\|JP2025117160 115628521 WHO=Applicant SELF=N	JP2000197810\|JP05212278\|JP2017109198\|JP2013504424\|JP03267120	JP2000197810 4041187 WHO=Examiner SELF=N CAT=Y\|JP05212278 13973977 WHO=Examiner SELF=N CAT=X CAT=Y\|JP2017109198 76580681 WHO=Examiner SELF=N\|JP2013504424 46598940 WHO=Applicant SELF=N\|JP03267120 28031985 WHO=Examiner SELF=N	特表２０１３－５０４４２４号公報\|Ｎｄｕａｇｕ，Ｅ．，Ｂｅｒｇｅｒｓｏｎ，Ｊ．ａｎｄＺｅｖｅｎｈｏｖｅｎ，Ｒ．，２０１２．ＬｉｆｅｃｙｃｌｅａｓｓｅｓｓｍｅｎｔｏｆＣＯ２ｓｅｑｕｅｓｔｒａｔｉｏｎｉｎｍａｇｎｅｓｉｕｍｓｉｌｉｃａｔｅｒｏｃｋＡｃｏｍｐａｒａｔｉｖｅｓｔｕｄｙ．ＥｎｅｒｇｙＣｏｎｖｅｒｓｉｏｎａｎｄＭａｎａｇｅｍｅｎｔ，５５，ｐｐ．１１６－１２６．\|Ｎｃｏｎｇｗａｎｅ，Ｍ．ｓ．，Ｂｒｏａｄｈｕｒｓｔ，Ｊ．Ｌ．ａｎｄＰｅｔｅｒｓｅｎ，Ｊ．，２０１８．ＡｓｓｅｓｓｍｅｎｔｏｆｔｈｅｐｏｔｅｎｔｉａｌｃａｒｂｏｎｆｏｏｔｐｒｉｎｔｏｆｅｎｇｉｎｅｅｒｅｄｐｒｏｃｅｓｓｅｓｆｗｏｒｔｈｅｍｉｎｅｒａｌｃａｒｂｏｎａｔｉｏｎｏｆＰＧＭｔａｉｌｉｎｇｓ．ＩｎｔｅｒｎａｔｉｏｎａｌＪｏｕｒｎａｌｏｆＧｒｅｅｎｈｏｕｓｅＧａｓＣｏｎｔｒｏｌ，７７，ｐｐ．７０－８１．\|Ｋｅｌｌｅｒ，ｄ．Ｐ．，Ｌｅｎｔｏｎ，Ａ．，Ｌｉｔｔｌｅｔｏｎ，Ｅ．ｗ．，Ｏｓｃｈｌｉｅｓ，Ａ．，Ｓｃｏｔｔ，ｖ．ａｎｄＶａｕｇｈａｎ，Ｎ．Ｅ．，２０１８．Ｔｈｅｅｆｆｅｃｔｓｏｆｃａｒｂｏｎｄｉｏｘｉｄｅｒｅｍｏｖａｌｏｎｔｈｅｃａｒｂｏｎｃｙｃｌｅ．Ｃｕｒｒｅｎｔｃｌｉｍａｔｅｃｈａｎｇｅｒｅｐｏｒｔｓ，４（３），ｐｐ．２５０－２６５．	JP05212278; JP2000197810; JP03267120; JP2017109198; 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date=2025-06-13\|Event code=JP/A61\|Event indicator=Pos\|Event group=Event indicating In Force\|First payment of annual fees (during grant procedure)\|Japanese intermediate code: A61\|Effective date of the event=2025-06-11\|Event publication date=2025-06-25\|Event code=JP/R150\|Event indicator=Pos\|Event group=Event indicating In Force\|CERTIFICATE OF PATENT OR REGISTRATION OF UTILITY MODEL\|Japanese intermediate code: R150\|Event publication date=2025-06-30\|Event code=JP/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Published granted patent (Second level) from 01-03-1996 onwards (Published examined patent application (Second level) 1971-1996)\|Publication country=JP\|Publication number=JP7699796\|Publication stage code=B2\|Publication date=2025-06-30\|Standardized publication number=JP7699796		(JP7699796)\|JP	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=e5gOkjdPC53qKdruKCQZdjeISh8T7V+NNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=JP0000000022803773&ekey=2281&xpn=JP7699796&kind=B2	https://www.j-platpat.inpit.go.jp/c1801/PU/JP-2021-075533/10/en	https://permalink.orbit.com/RenderStaticFirstPage?XPN=PBN44GkNLeTWqxLm4QBXD3fDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	JP				(JP7699796)\|NAME=HATA, Masanori , REG=100115842\|(JP2022169854)\|NAME=HATA, Masanori , REG=100115842		(JP7699796)\|NAME=Myers, Corey Adam\|NAME=NAKAGAKI Takao\|(JP2022169854)\|NAME=COREY ADAM MYERS\|NAME=NAKAGAKI TAKAO	(JP7699796)\|2	1	1					(JP7699796)\|Number of Claims: NCL=4\|Form: FORM=OL\|Request for examination: REQEXA=false\|Primary examiner: 駒木亮一\|\|(JP2022169854)\|Number of Claims: NCL=7\|Form: FORM=OL\|Request for examination: REQEXA=false\|Primary examiner: 駒木亮一\|	(JP7699796)\|Previous publication: JP2022169854 2022-11-10 [JP2022169854]	(JP7699796)\|JAPANESE (JPN)	(JP7699796)\|Patent\|(JP2022169854)\|Patent	Titre: (JP7699796)\|How to remove carbon dioxide from the air Résumé: (JP7699796)\|PROBLEM TO BE SOLVED: To provide a method which can be executed at low cost, can substantially reduce carbon dioxide, and removes carbon dioxide in the air friendly to an environment with no risk of storing the carbon dioxide.SOLUTION: The present invention atomizes a rock containing an alkaline earth metal, immobilizes carbon dioxide to the rock by bringing acquired fine particles into contact with the air in a space as prescribed environment to mineralize carbon dioxide in the air as carbonate, and removes the carbon dioxide in the air. The invention can easily remove the carbon dioxide in the air at low cost without using chemical, and can remove qualitative carbon dioxide with little production amount of accompanying carbon dioxide. In addition, the immobilized carbon dioxide becomes carbonate harmless to environment and friendly to the environment with no risk of storing the carbon dioxide.SELECTED DRAWING: Figure 1COPYRIGHT: (C)2023,JPO&INPIT	44	Abstract	gpt-4o-mini	yes	The patent describes a method for mineralizing CO₂ using alkaline earth metal-containing rocks, which aligns with the goal of enhanced weathering and carbon sequestration.
45	EP12306468	EP12306468	EP2735553\|EP2735553	66070146	EP2735553 B1 2017-04-05 [EP2735553]\|EP2735553 A1 2014-05-28 [EP2735553]	2012-11-27	2012-11-27	2017-04-05\|2014-05-28	(EP2735553)\|2017-04-05	(EP2735553)\|2020-10-30	(EP2735553)\|Process for the treatment of a silicate mineral	(EP2735553)\|The invention provides a process for the preparation of a first product comprising an alkali metal magnesium orthosilicate and (i) magnesium oxide or (ii) an alkali metal silicate, which process comprises the reaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R 2 O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO 2 , being from 4:1 to 1:4, and contacting the first product with water to produce a second product comprising magnesium hydroxide and isolating or producing further useful products from the second product.	LAFARGE	(EP2735553)\|LAFARGE ([FR])\|(EP2735553)\|LAFARGE ([FR])	GARTNER ELLIS\|PISCH ALEXANDER\|MEYER VINCENT	(EP2735553)\|Gartner, Ellis\|Pisch, Alexander\|Meyer, Vincent\|(EP2735553)\|Gartner, Ellis\|Pisch, Alexander\|Meyer, Vincent	(EP2735553)\|Keschmann, Marc;Haffner und Keschmann ([AT])\|Reg. Nb: 101393339	(EP2735553)\|However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible.\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled.\|Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300°C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eiteleite, Na2CO3*MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|	(EP2735553)\|1. A process for the treatment of a silicate mineral comprising: - a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate and a magnesium oxide, which step comprising the reaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula F2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, - a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate,and - a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product\|	(EP2735553)\|The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|The present invention accordingly provides a process for the treatment of a silicate mineral comprising a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate of the general formula R2MgSiO4 wherein R represents an alkali metal, and magnesium oxide which process comprises the reaction, at a temperature from 500 to 200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate, and a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product.\|This invention relates to a process for the treatment of a silicate mineral, The process uses as starting material a magnesium silicate and produces an alkali metal magnesium orthosilicate and magnesium oxide each of which can be isolated or subjected to further treatment to produce other products.\|	(EP2735553)\|SILICATE MINERAL(100,4)\|SILICATE MINERAL TREATMENT(100,4)\|MAGNESIA(97,20)\|MAGNESIUM ORTHOSILICATE(89,16)\|AMORPHOUS SILICA PRECIPITATE(79,2)\|MAGNESIUM SILICATE(72,49)\|SILICA PRECIPITATE(70,1)\|OUTGOING HOT GAS(64,1)\|MOVING GRATE FURNACE(62,2)\|MAGNESIUM OXIDE(58,25)\|OUTGOING HOT SOLID(58,1)\|ALKALI METAL CARBONATE(56,49)\|PRODUCT CARBONATION(56,4)\|MOLAR RATIO(53,10)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(50,11)\|NEUTRALIZING(50,1)\|ALKALI METAL(48,75)\|EITELEITE(48,1)\|INCOMING SOLID(48,1)\|IRON ISOLATION(48,1)\|ALKALI METAL DISSOLUTION(46,3)\|ALKALI METAL BICARBONATE(44,4)\|FURNACE(42,8)\|NA2CO(40,1)\|MOVING GRATE(38,5)\|INCOMING COMBUSTION AIR(38,1)\|NET ENERGY CONSUMPTION(36,2)\|USEFUL PRODUCT(36,2)\|TEMPERATURE ELEVATION(36,1)\|METHANEDIONE(35,5)\|COUNTERCURRENT HEAT EXCHANGE(35,3)\|CHROMIUM COMPOUND(35,2)\|PELLET(29,16)\|AMBIENT TEMPERATURE(28,2)\|MAGNESIUM OXIDE MOLAR RATIO(28,1)\|CO2(27,22)\|DEHYDRATION(26,2)\|UNREACTED OLIVINE(24,3)\|COMPLEX ALKALI METAL(24,1)\|MGCO(23,8)\|BED(23,5)\|HEAT EXCHANGE(22,4)\|PREHEATER CYCLONE TOWER(22,1)\|ALKALI METAL SILICATE(21,7)\|LAB FURNACE(20,4)\|OLIVINE SAND(20,3)\|PLATINUM CRUCIBLE(20,3)\|PHOTOMETRY HYDROMAGNESITE MG(20,1)\|SOLID PRODUCT(19,11)\|XRF SPECTROMETRY(19,2)\|GASEOUS CO2(18,4)\|ASBESTOS FIBRILLAR(18,1)\|DECARBONATED NODULE(18,1)\|OBSCURATION STABILIZATION(18,1)\|HYDRAULIC BINDER(17,3)\|HYDROMAGNE SITE(17,3)\|FINE SUSPENSION(16,4)\|EARTH CRUST(16,2)\|LASER GRANULOMETRY(16,2)\|RESIDUAL R2CO(16,2)\|CENTRATE TAILING(16,1)\|COUNTER CURRENT HEAT EXCHANGE(16,1)\|DECARBONATED PELLET(16,1)\|METHANEDIONE GAS LIBERATION(16,1)\|ANHYDROUS MAGNESIUM SILICATE(14,2)\|SI CA MG(14,2)\|ABSORB METHANEDIONE(14,1)\|CO2 NET CONSUMER(14,1)\|CO2 SEQUESTRATION(14,1)\|DISSOLUTION BEHAVIOR(14,1)\|HEAT TRANSFER(14,1)\|HELICOIDAL TEFLON(14,1)\|MAGNETITE TRACE(14,1)\|METHANEDIONE EVAPORATION(14,1)\|MINIATURE FLOTATION CELL(14,1)\|PREHEATER TOWER(14,1)\|SILICATE HYDROPHOBICITY(14,1)\|ANHYDROUS PRODUCT(13,5)\|ARTINITE(13,5)\|AUTOCLAVE(13,5)\|FILTER CAKE DRYING(13,5)\|FORSTERITE(13,4)\|ENERGY EFFICIENCY(13,3)\|SAMPLE REACTION(13,3)\|FE2O(12,9)\|EITELITE(12,4)\|MG2SIO(12,4)\|NA2MGSIO(12,4)\|PARTICULATE(12,4)\|POWDERED PRODUCT(12,4)\|PRODUCT RICH(12,4)\|BURNING ZONE(12,2)\|TRANSITION METAL(12,2)\|CARBONATE PARTICLE(12,1)\|CONCENTRATE CO2 CONTENT(12,1)\|ENHANCE NA RECYCLING(12,1)\|EXPERIMENT MULTIPLIER(12,1)\|GROUND OLIVINE MIX(12,1)\|LASER GRANULOMETER(12,1)\|NODULE RISK(12,1)\|PERFECTLY BALANCED EQUATION(12,1)\|PRINCIPAL DISSOLVED ANION(12,1)\|PRODUCT HECTORITE MANUFACTURER(12,1)\|SAMPLE DEAGGLOMERATION(12,1)\|SUSPENSION PREHEATER(12,1)\|UNREACTED ANHYDROUS COMPOUND(12,1)\|UNTREATED RESIDUE(12,1)\|COLORLESS SOLUTION(11,2)\|ESTIMATED MG(11,2)\|GAS ANALYZER(11,2)\|MAGNESIUM OXIDE HYDRATION(11,2)\|REACTED SAMPLE PHASE CONSTITUTION(11,2)\|REACTION PRODUCT(10,7)\|ALKALI METAL OXIDE(10,6)\|ALKALINE SOLUTION(10,3)\|COMBUSTION EXHAUST GAS(10,3)\|HYDROCYCLONE(10,3)\|NESQUEHONITE(10,3)\|PERICLASE(10,3)\|QUENCHING(10,3)\|AMORPHOUS MAGNESIUM SILICATE(10,1)\|CO2 EMISSION(10,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(10,1)\|DECARBONATION REACTION(10,1)\|EARTH MANTLE COMPONENT(10,1)\|FERMENTATION RESIDUE GAS(10,1)\|FINE NESS(10,1)\|FINE SAND GRANULOMETRY(10,1)\|FLOTATION AID(10,1)\|INORGANIC IMPURITY(10,1)\|LAYERED DOUBLE HYDROXIDE(10,1)\|MINERAL CARBONATE(10,1)\|MOVING GRATE COOLER(10,1)\|OLIVINE SAMPLE(10,1)\|PRECIPITATED SILICA(10,1)\|R2O MOLAR RATIO(10,1)\|RAW MAGNESIUM SILICATE(10,1)\|ROCK SPECIES(10,1)\|SLURRY CONC(10,1)\|SODIUM SILICATE MILIMOLE LITER(10,1)\|SUSPENSION AGITATION(10,1)\|SYNTHETIC HECTORITE(10,1)\|UNREACTED MAGNESIUM SILICATE(10,1)\|UNREACTED PARTICLE(10,1)\|VESSEL PRESSURIZATION(10,1)\|WORKING SESSION(10,1)\|NA2O(9,4)\|CARBOXYMETHYLCELLULOSE(9,3)\|MAGNESIUM SILICATE WATER(8,5)\|SODIUM OLEATE(8,5)\|CEMENT PLANT(8,4)\|HOT GAS(8,4)\|R2SIO(8,4)\|ROTARY KILN(8,4)\|ACTINOLITE(8,2)\|AMOSITE(8,2)\|AMPHIBOLE(8,2)\|ANHYDROUS SODIUM CARBONATE(8,2)\|BRUCITE(8,2)\|CENTRIFUGATION(8,2)\|CHRYSOTILE(8,2)\|COMPLEX MAGNESIUM(8,2)\|CRYSTALLINE PHASE(8,2)\|ENSTATITE(8,2)\|FILTER CAKE MG(8,2)\|LIQUID FILTRATE(8,2)\|MEASURED LOI DATA(8,2)\|MG CONTENT(8,2)\|MGO SILICA MOLAR RATIO(8,2)\|MIXED POWDER(8,2)\|MR2MGSIO(8,2)\|PYROXENE(8,2)\|SIEVING(8,2)\|SODIUM CARBONATE POWDER(8,2)\|SYMBOL(8,2)\|TREMOLITE(8,2)\|ULTRASOUND(8,2)\|ALKALI BICARBONATE SOLUTION(8,1)\|ALKALI MAGNESIUM METAL ORTHOSILICATE(8,1)\|ALKALI SOLUBLE IMPURITY(8,1)\|BASIC MAGNESIUM ORTHOSILICATE(8,1)\|BIOMASS DERIVED FUEL(8,1)\|BLUE DIODE(8,1)\|CALCULATION MATRIX(8,1)\|CARBONATABLE SOLID(8,1)\|CARBONATE ION(8,1)\|CARBONATED PRODUCT(8,1)\|CHROMIUM CONTENT(8,1)\|CO2 GRAM(8,1)\|COARSE UNREACTED SOLID(8,1)\|COMBINED CO2 QUANTITATIVE DETECTION(8,1)\|COOLED PELLET(8,1)\|CRUSHED SAMPLE(8,1)\|HOT NODULE HEAT(8,1)\|HOT QUENCHED SOLID(8,1)\|INCOMING COMBUSTION AIR PREHEATER(8,1)\|MAGNESIA FINE PARTICLE(8,1)\|MAGNESIUM SILICATE MINERAL(8,1)\|MAJOR IMPURITY(8,1)\|MAXIMUM CO2 CAPTURE(8,1)\|MAXIMUM SLURRY ADDITIVE(8,1)\|NATURAL TALC(8,1)\|NATURALLY OCCURRING MINERAL(8,1)\|OUTGOING SOLID PARTICLE(8,1)\|PHASE PROBABILITY(8,1)\|PLUS MAGNESIUM(8,1)\|POROUS BED(8,1)\|POWDER SELF NODULIZE(8,1)\|PREHEATER TOP CYCLONE(8,1)\|QUALITATIVE PHASE(8,1)\|QUICK WASH(8,1)\|REACTION ESCAPE(8,1)\|REACTOR CONTENT(8,1)\|RED HE NE LASER(8,1)\|SESQUIHYDRATE(8,1)\|SILICA MOLE(8,1)\|SODIUM HYDROXIDE MILLIMOLE LITER(8,1)\|SOLUBLE SALT(8,1)\|SORT REACTION(8,1)\|STEEL CRUCIBLE(8,1)\|SULFUR CONTENT(8,1)\|TABLE EXPERIMENT(8,1)\|TREATED PELLET(8,1)\|TREATED SLURRY(8,1)\|WEAK PEAK(8,1)\|XRD DATA RIETVELD ANALYSIS(8,1)\|METHYL ISOBUTYL CARBINOL(7,5)\|NAFEO(7,2)\|SIEVE(7,2)\|DEIONIZED WATER(6,4)\|ATMOSPHERE PRESSURE(6,3)\|FE3O(6,3)\|H2SIO(6,3)\|HYDROXY CARBONATE WATER(6,3)\|USEFUL PRODUCT STREAM(6,3)\|XH2O(6,3)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|AIR BUBBLING(6,1)\|ALKALINE AQUEOUS SOLUTION(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANTHOPHYLLITE(6,1)\|ANTIGORITE(6,1)\|AQUEOUS ACID(6,1)\|AQUEOUS PHASE ICP ANALYSIS(6,1)\|ARLTHOPHYLLITE(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|CALCINATION(6,1)\|CAO SILICA MOLAR RATIO(6,1)\|CARBONATE PRODUCT(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|CRYSTALLINE PRODUCT(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|DURATIO N(6,1)\|EXCESS FERROUS SULFATE(6,1)\|FAYALITE(6,1)\|FE2SIO(6,1)\|\|(EP2735553)\|SILICATE MINERAL(100,4)\|SILICATE MINERAL TREATMENT(100,4)\|MAGNESIA(97,20)\|MAGNESIUM ORTHOSILICATE(89,16)\|AMORPHOUS SILICA PRECIPITATE(79,2)\|MAGNESIUM SILICATE(72,49)\|SILICA PRECIPITATE(70,1)\|OUTGOING HOT GAS(64,1)\|MOVING GRATE FURNACE(62,2)\|MAGNESIUM OXIDE(58,25)\|OUTGOING HOT SOLID(58,1)\|ALKALI METAL CARBONATE(56,49)\|PRODUCT CARBONATION(56,4)\|MOLAR RATIO(53,10)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(50,11)\|NEUTRALIZING(50,1)\|ALKALI METAL(48,75)\|EITELEITE(48,1)\|INCOMING SOLID(48,1)\|IRON ISOLATION(48,1)\|ALKALI METAL DISSOLUTION(46,3)\|ALKALI METAL BICARBONATE(44,4)\|FURNACE(42,8)\|NA2CO(40,1)\|MOVING GRATE(38,5)\|INCOMING COMBUSTION AIR(38,1)\|NET ENERGY CONSUMPTION(36,2)\|USEFUL PRODUCT(36,2)\|TEMPERATURE ELEVATION(36,1)\|METHANEDIONE(35,5)\|COUNTERCURRENT HEAT EXCHANGE(35,3)\|CHROMIUM COMPOUND(35,2)\|PELLET(29,16)\|AMBIENT TEMPERATURE(28,2)\|MAGNESIUM OXIDE MOLAR RATIO(28,1)\|CO2(27,22)\|DEHYDRATION(26,2)\|UNREACTED OLIVINE(24,3)\|COMPLEX ALKALI METAL(24,1)\|MGCO(23,8)\|BED(23,5)\|HEAT EXCHANGE(22,4)\|PREHEATER CYCLONE TOWER(22,1)\|ALKALI METAL SILICATE(21,7)\|LAB FURNACE(20,4)\|OLIVINE SAND(20,3)\|PLATINUM CRUCIBLE(20,3)\|PHOTOMETRY HYDROMAGNESITE MG(20,1)\|SOLID PRODUCT(19,11)\|XRF SPECTROMETRY(19,2)\|GASEOUS CO2(18,4)\|ASBESTOS FIBRILLAR(18,1)\|DECARBONATED NODULE(18,1)\|OBSCURATION STABILIZATION(18,1)\|HYDRAULIC BINDER(17,3)\|HYDROMAGNE SITE(17,3)\|FINE SUSPENSION(16,4)\|EARTH CRUST(16,2)\|LASER GRANULOMETRY(16,2)\|RESIDUAL R2CO(16,2)\|CENTRATE TAILING(16,1)\|COUNTER CURRENT HEAT EXCHANGE(16,1)\|DECARBONATED PELLET(16,1)\|METHANEDIONE GAS LIBERATION(16,1)\|ANHYDROUS MAGNESIUM SILICATE(14,2)\|SI CA MG(14,2)\|ABSORB METHANEDIONE(14,1)\|CO2 NET CONSUMER(14,1)\|CO2 SEQUESTRATION(14,1)\|DISSOLUTION BEHAVIOR(14,1)\|HEAT TRANSFER(14,1)\|HELICOIDAL TEFLON(14,1)\|MAGNETITE TRACE(14,1)\|METHANEDIONE EVAPORATION(14,1)\|MINIATURE FLOTATION CELL(14,1)\|PREHEATER TOWER(14,1)\|SILICATE HYDROPHOBICITY(14,1)\|ANHYDROUS PRODUCT(13,5)\|ARTINITE(13,5)\|AUTOCLAVE(13,5)\|FILTER CAKE DRYING(13,5)\|FORSTERITE(13,4)\|ENERGY EFFICIENCY(13,3)\|SAMPLE REACTION(13,3)\|FE2O(12,9)\|EITELITE(12,4)\|MG2SIO(12,4)\|NA2MGSIO(12,4)\|PARTICULATE(12,4)\|POWDERED PRODUCT(12,4)\|PRODUCT RICH(12,4)\|BURNING ZONE(12,2)\|TRANSITION METAL(12,2)\|CARBONATE PARTICLE(12,1)\|CONCENTRATE CO2 CONTENT(12,1)\|ENHANCE NA RECYCLING(12,1)\|EXPERIMENT MULTIPLIER(12,1)\|GROUND OLIVINE MIX(12,1)\|LASER GRANULOMETER(12,1)\|NODULE RISK(12,1)\|PERFECTLY BALANCED EQUATION(12,1)\|PRINCIPAL DISSOLVED ANION(12,1)\|PRODUCT HECTORITE MANUFACTURER(12,1)\|SAMPLE DEAGGLOMERATION(12,1)\|SUSPENSION PREHEATER(12,1)\|UNREACTED ANHYDROUS COMPOUND(12,1)\|UNTREATED RESIDUE(12,1)\|COLORLESS SOLUTION(11,2)\|ESTIMATED MG(11,2)\|GAS ANALYZER(11,2)\|MAGNESIUM OXIDE HYDRATION(11,2)\|REACTED SAMPLE PHASE CONSTITUTION(11,2)\|REACTION PRODUCT(10,7)\|ALKALI METAL OXIDE(10,6)\|ALKALINE SOLUTION(10,3)\|COMBUSTION EXHAUST GAS(10,3)\|HYDROCYCLONE(10,3)\|NESQUEHONITE(10,3)\|PERICLASE(10,3)\|QUENCHING(10,3)\|AMORPHOUS MAGNESIUM SILICATE(10,1)\|CO2 EMISSION(10,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(10,1)\|DECARBONATION REACTION(10,1)\|EARTH MANTLE COMPONENT(10,1)\|FERMENTATION RESIDUE GAS(10,1)\|FINE NESS(10,1)\|FINE SAND GRANULOMETRY(10,1)\|FLOTATION AID(10,1)\|INORGANIC IMPURITY(10,1)\|LAYERED DOUBLE HYDROXIDE(10,1)\|MINERAL CARBONATE(10,1)\|MOVING GRATE COOLER(10,1)\|OLIVINE SAMPLE(10,1)\|PRECIPITATED SILICA(10,1)\|R2O MOLAR RATIO(10,1)\|RAW MAGNESIUM SILICATE(10,1)\|ROCK SPECIES(10,1)\|SLURRY CONC(10,1)\|SODIUM SILICATE MILIMOLE LITER(10,1)\|SUSPENSION AGITATION(10,1)\|SYNTHETIC HECTORITE(10,1)\|UNREACTED MAGNESIUM SILICATE(10,1)\|UNREACTED PARTICLE(10,1)\|VESSEL PRESSURIZATION(10,1)\|WORKING SESSION(10,1)\|NA2O(9,4)\|CARBOXYMETHYLCELLULOSE(9,3)\|MAGNESIUM SILICATE WATER(8,5)\|SODIUM OLEATE(8,5)\|CEMENT PLANT(8,4)\|HOT GAS(8,4)\|R2SIO(8,4)\|ROTARY KILN(8,4)\|ACTINOLITE(8,2)\|AMOSITE(8,2)\|AMPHIBOLE(8,2)\|ANHYDROUS SODIUM CARBONATE(8,2)\|BRUCITE(8,2)\|CENTRIFUGATION(8,2)\|CHRYSOTILE(8,2)\|COMPLEX MAGNESIUM(8,2)\|CRYSTALLINE PHASE(8,2)\|ENSTATITE(8,2)\|FILTER CAKE MG(8,2)\|LIQUID FILTRATE(8,2)\|MEASURED LOI DATA(8,2)\|MG CONTENT(8,2)\|MGO SILICA MOLAR RATIO(8,2)\|MIXED POWDER(8,2)\|MR2MGSIO(8,2)\|PYROXENE(8,2)\|SIEVING(8,2)\|SODIUM CARBONATE POWDER(8,2)\|SYMBOL(8,2)\|TREMOLITE(8,2)\|ULTRASOUND(8,2)\|ALKALI BICARBONATE SOLUTION(8,1)\|ALKALI MAGNESIUM METAL ORTHOSILICATE(8,1)\|ALKALI SOLUBLE IMPURITY(8,1)\|BASIC MAGNESIUM ORTHOSILICATE(8,1)\|BIOMASS DERIVED FUEL(8,1)\|BLUE DIODE(8,1)\|CALCULATION MATRIX(8,1)\|CARBONATABLE SOLID(8,1)\|CARBONATE ION(8,1)\|CARBONATED PRODUCT(8,1)\|CHROMIUM CONTENT(8,1)\|CO2 GRAM(8,1)\|COARSE UNREACTED SOLID(8,1)\|COMBINED CO2 QUANTITATIVE DETECTION(8,1)\|COOLED PELLET(8,1)\|CRUSHED SAMPLE(8,1)\|HOT NODULE HEAT(8,1)\|HOT QUENCHED SOLID(8,1)\|INCOMING COMBUSTION AIR PREHEATER(8,1)\|MAGNESIA FINE PARTICLE(8,1)\|MAGNESIUM SILICATE MINERAL(8,1)\|MAJOR IMPURITY(8,1)\|MAXIMUM CO2 CAPTURE(8,1)\|MAXIMUM SLURRY ADDITIVE(8,1)\|NATURAL TALC(8,1)\|NATURALLY OCCURRING MINERAL(8,1)\|OUTGOING SOLID PARTICLE(8,1)\|PHASE PROBABILITY(8,1)\|PLUS MAGNESIUM(8,1)\|POROUS BED(8,1)\|POWDER SELF NODULIZE(8,1)\|PREHEATER TOP CYCLONE(8,1)\|QUALITATIVE PHASE(8,1)\|QUICK WASH(8,1)\|REACTION ESCAPE(8,1)\|REACTOR CONTENT(8,1)\|RED HE NE LASER(8,1)\|SESQUIHYDRATE(8,1)\|SILICA MOLE(8,1)\|SODIUM HYDROXIDE MILLIMOLE LITER(8,1)\|SOLUBLE SALT(8,1)\|SORT REACTION(8,1)\|STEEL CRUCIBLE(8,1)\|SULFUR CONTENT(8,1)\|TABLE EXPERIMENT(8,1)\|TREATED PELLET(8,1)\|TREATED SLURRY(8,1)\|WEAK PEAK(8,1)\|XRD DATA RIETVELD ANALYSIS(8,1)\|METHYL ISOBUTYL CARBINOL(7,5)\|NAFEO(7,2)\|SIEVE(7,2)\|DEIONIZED WATER(6,4)\|ATMOSPHERE PRESSURE(6,3)\|FE3O(6,3)\|H2SIO(6,3)\|HYDROXY CARBONATE WATER(6,3)\|USEFUL PRODUCT STREAM(6,3)\|XH2O(6,3)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|AIR BUBBLING(6,1)\|ALKALINE AQUEOUS SOLUTION(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANTHOPHYLLITE(6,1)\|ANTIGORITE(6,1)\|AQUEOUS ACID(6,1)\|AQUEOUS PHASE ICP ANALYSIS(6,1)\|ARLTHOPHYLLITE(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|CALCINATION(6,1)\|CAO SILICA MOLAR RATIO(6,1)\|CARBONATE PRODUCT(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|CRYSTALLINE PRODUCT(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|DURATIO N(6,1)\|EXCESS FERROUS SULFATE(6,1)\|FAYALITE(6,1)\|FE2SIO(6,1)\|	(EP2735553)\|1. A process for the treatment of a silicate mineral comprising:\| - a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate and a magnesium oxide, which step comprising the reaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula F2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4,\| - a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate,\|and\| - a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product\|2. A process according to claim 1 in which the magnesium silicate is a magnesium silicate in which the molar ratio of magnesium oxide to silica is from 1 to 3.\|3. A process according to any one of claims 1 to 2 in which the magnesium silicate comprises a magnesium silicate rock of the general composition:\| m(MgO)•t(QO)•SiO2•xH2O\|wherein m is from 1 to 3, t is less than or equal to 1, x is from zero to 2, and Q represents a metal or metals other than magnesium.\|4. A process according to any one of the preceding claims further comprising subsequent steps of (i) carbonation of the second product to produce a carbonated third product and (ii) partial dehydration of the carbonated third product to produce a fourth product.\|5. A process according to any one of claims 1 to 3 further comprising subsequent steps of (i) carbonation of the second product to produce a third product comprising magnesium hydroxide and an alkali metal carbonate and (ii) calcining the magnesium hydroxide in the third product to produce a fifth product comprising magnesium oxide.\|6. A process according to claim 3 in which Q represents iron, nickel and/or chromium which process further comprises isolation of an iron, nickel or chromium compound,	(EP2735553)\|[0001] This invention relates to a process for the treatment of a silicate mineral, The process uses as starting material a magnesium silicate and produces an alkali metal magnesium orthosilicate and magnesium oxide each of which can be isolated or subjected to further treatment to produce other products.\|[0002] US5085838 discloses preparation of a product comprising an alkali metal magnesium orthosilicate and a magnesium oxide, in which an alkali metal carbonate compound is reacted with a magnesium silicate.\|[0003] US2012291675 and US2004213705 describe processes for the sequestration of CO2 WO20070159902 discloses a method for industrial manufacture of pure MgCO3 from an olivine containing species of rock.\|[0004] XP2994928 describes a process where sodium bicarbonate, sodium chloride and water are mixed with magnesium silicates.\|[0005] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into common magnesium silicate hydrate minerals such as serpentine (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10(OH)2). Magnesium silicate rocks constitute an excellent source of two important elements, magnesium and silicon, in their oxide forms (MgO and SiO2). Processes to extract these two oxides from such rocks have heretofore been excessively energy-intensive and thus have not been commercialized.\|[0006] Although the magnesium silicate minerals tend to be very "unreactive," (e,g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a "carbonate fusion", is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analyzed by standard chemical techniques, thus allowing for total elemental analysis of the rock The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0007] The term sodium magnesium silicate is sometimes used, in accordance with the International Nomenclature of Cosmetic Ingredients (INCI) to identify synthetic hectorites in the form of nanoparticles and which form clear gels in water According to one manufacturer of such products hectorites have the formula (Mg5.2Li0.8)(Si8)O20(OH)4Na0.8.\|[0008] The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|[0009] The present invention accordingly provides a process for the treatment of a silicate mineral comprising a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate of the general formula R2MgSiO4 wherein R represents an alkali metal, and magnesium oxide which process comprises the reaction, at a temperature from 500 to 200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate, and a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product.\|[0010] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate, expressed as silicon dioxide, is preferably from <4:1 to 1:4, more preferably from 3:1 to 1:3, for example 2:1 to 1:2. The ratio is most preferably about 1.\|[0011] The alkali metal is preferably potassium or, more preferably, sodium.\|[0012] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used in the process of the invention.\|[0013] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0014] The magnesium silicate used in the process of the invention is generally a mineral silicate, for example a rock comprising a high concentration, preferably 20% or more, more preferably 50% or more, of a magnesium silicate of general composition:\| m(MgO)•t(QO)•SiO3•xH2O\|wherein m is from 1 to 3, t is less than or equal to 1, and x is from zero to 2: and Q represents a metal or metals other than magnesium, (for example calcium and/or a transition group metal such as iron, chromium or nickel). It will be understood that the composition or formulae of minerals is often depicted in terms of the theoretical amount of oxides which they contain: the oxides are, however, not present as such in the minerals whose composition is depicted in this way.\|[0015] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc, iddingsite and hectorite. These minerals may contain substantial quantities of iron in addition to magnesium and silicon, and also significant amounts of calcium, aluminium and alkali metals,\|[0016] Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, arlthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0017] The mineral silicate used in the process of the invention is preferably a magnesium silicate. The MgO/SiO2 molar ratio is 1-3. The CaO/SiO2 molar ratio is preferably ≤0.5. The FeO/SiO2 molar ratio is preferably ≤0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≤0.2.\|[0018] The alkali metal carbonate compound used in the process of the invention may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2•2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g chlorides, sulfates, sulphites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates or hydroxides) are present which, at the temperature used in the process of the invention, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0019] The process of the invention is preferably effected at a temperature from 600 to 1100°C, more preferably from 800 to 1000°C. Heating is generally effected for a few minutes to a few hours.\|[0020] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is solid or liquid.\|[0021] According to a feature of the invention the process is effected at a temperature below the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound.\|[0022] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as "R2O" in which R is as hereinbefore defined present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt. = 140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt. = 106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0023] The magnesium silicate and alkali metal carbonate compound used in the process of the present invention are preferably in particulate form or in shaped form, e.g. as pellets.\|[0024] Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the process of the invention will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of a fine sand (grain size 0.06 to 0.2mm) or, if necessary, ground to a fine powder (grain sizes below 0.06mm). Grain sizes greater than 0.06mm are generally determined by sieving. Grain sizes lower than 0.06mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0025] In one embodiment the process of the invention is conducted in a moving grate furnace. This procedure is especially suited to magnesium silicate rocks (rocks comprising mainly MgO and SiO2) in which the MgO/SiO2 molar ratio is close to or greater than 1.\|[0026] A mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in Figure 1 of the accompanying drawings.\|[0027] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0028] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone ("burning zone") just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1a) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate (R2CO3)\| (1a) Mg2SiO4 + R2CO3 ⇒ MgO + R2MgSiO4 + CO2↑\|in which R is as hereinbefore defined. The more general form of this reaction can be written as in equation (1 b) for m>=1 and equation 1 (c) for m<1:\| (1b) m(MgO)•t(QO)•SiO2•xH2O + R2CO3 ⇒ (m-1)MgO + R2MgSiO4 + tQO + CO2↑ + xH2O↑\| (1c) m(MgO)•t(QO)•SiO2•xH2O + R2CO3 ⇒ (1-m)R2SiO3 + mR2MgSiO4 + tQO + CO2↑ + xH2O↑\|wherein m is greater than or equal to 1 for reaction (1 b) and less than or equal to 1 for reaction (1 c); and Q, t and x are as hereinbefore defined. The vertical arrows T indicate that the carbon dioxide gas and water vapour produced by this reaction escape from the bed and exits with the rest of the exhaust gases. Thus, ideally, the final solid product remaining in the treated pellets is an intimate mixture comprising magnesium oxide (MgO also known as periclase) and alkali metal magnesium orthosilicate (R2MgSiO4) and/or alkali metal silicates (R2SiO3) as well as other solid products comprising the other metals (Q), especially iron, which may present as magnetite (Fe3O4) or possibly as an alkali metal ferrite (RFeO2), calcium, which may be present as silicates, chromium, which may be present as alkali metal chromates (R2CrO4), and nickel, which may be present as oxides.\|[0029] The idealized reactions depicted in equations (1 a,b,c) illustrate the production of alkali metal magnesium orthosilicates plus magnesium and/or other oxides and silicates by direct reaction of a stoichiometric (i.e. 1:1 R2O:SiO2) mixture of a magnesium silicate and an alkali metal carbonate.\|[0030] This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 3.4 kJ (i.e. about 0.8 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, there will be a significant net energy consumption for the overall process. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0031] In a further embodiment, the process of the invention is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln for the process of the invention which comprises a decarbonation step which produces carbon dioxide.\|[0032] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0033] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 35% of the total solids volume. However, since the reaction itself produces no liquid products (only solids and gases) at the temperatures preferably employed, the risk of the nodules deforming significantly due to melting is quite low even at far higher initial volume fractions of alkali metal carbonate as long as the heating occurs slowly enough to allow for a significant degree of reaction to occur before complete melting of the alkali metal carbonate.\|[0034] According to a further feature of the invention the process of the invention is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The nodules are then decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0035] The decarbonated and cooled pellets or nodules, comprising alkali metal magnesium orthosilicate and magnesium oxide or alkali metal silicate, are treated in order to separate the reaction products.\|[0036] In the process of the invention the first product comprising alkali metal magnesium orthosilicate and magnesium oxide is contacted with water to form a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate.\|[0037] The first product as, for example pellets or nodules, is preferably quenched in an amount of water, such that the final mixture after quenching has a temperature close to, but not exceeding, about 100°C, i.e. enough to quench the solids but avoiding excessive evaporation of water. The hot quenched solids are then preferably crushed and agitated mechanically in the form of a slurry. More water may be added if necessary. Some additional heating may be necessary.\|[0038] Alternatively the treatment with water, for example in the quenching and slurry-formation process described above, can be conducted at a temperature above 100°C if a pressurized vessel (e.g. an autoclave) is used.\|[0039] Alternatively the above quenching and slurry-formation process can be conducted at lower or ambient temperatures. Water for converting the first product into the second product can optionally be recycled from another part of the process.\|[0040] The objective is to separate the components of the second product by virtue of the facts that (a) alkali metal carbonates, silicates, chromates, sulfates and oxides or hydroxides in the product will tend to dissolve readily in water; (b) alkali metal magnesium orthosilicates will tend to hydrate in hot water to release alkali metals into solution as silicates and hydroxides, the remainder giving a fine suspension of solid magnesium silicate hydrates, and (c) magnesium oxide (MgO, also known as periclase) in the sample will tend to hydrate in hot water to give magnesium hydroxide (Mg(OH)2, also known as brucite) to form a soft and easily-dispersible powder.\|[0041] The slurry may need to be agitated mechanically. Then, the liquid phase can be separated from the bulk of the unreacted alkali metal magnesium orthosilicate and other unreacted anhydrous compounds, for example by sieving, and the fine particles of magnesium hydroxide and/or magnesium silicate hydrates which pass through the sieve as a slurry may be separated from the slurry by, for example, filtering, passage through a hydrocyclone, settling and/or centrifuging. The aqueous phase after separation of the magnesium hydroxide comprises an aqueous solution of alkali metal silicates and hydroxides.\|[0042] Alternatively, the separation process may be conducted in two steps, the first step comprising a rapid washing process to remove most of the readily soluble alkali metal carbonates, silicates and hydroxides; and the second step, conducted with additional water, comprising further hydration of both the magnesium oxide and the alkali metal magnesium orthosilicate. In this two-step approach, the water temperature is preferably lower for the first step (for example lower than 60°C) than for the second step, and an autoclave may be used for the second step if necessary.\|[0043] The overall result of the separation process described above can be summarized as follows: Solid products from the process of the invention, e.g. from the furnace or kiln, (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4, MgO or R2SiO3, QO, and possibly some residual R2CO3) are contacted with water to produce a second product comprising:\| (a) a fine suspension comprising Mg(OH)2 and/or magnesium silicate hydrates in a highly alkaline solution rich in alkali metal silicates, hydroxides and carbonates, and\| (b) coarse unreacted solids comprising R2MgSiO4, MgO, QO and unreacted particles of the original magnesium silicate rock (e.g. Mg2SiO4), and which separate easily by sedimentation (e.g. in a hydrocyclone) from the fine suspension.\|The fine suspension can then be further separated (e.g. by filtration) to give\| (c) fine solids rich in Mg(OH)2 and/or magnesium silicate hydrates, and\| (d) a solution rich in alkali metal silicates, hydroxides and carbonates, and also comprising minor amounts of alkali-soluble impurities, e.g. sulfates and chromates.\|[0044] The initial part of the reaction of the solid products in the process with water can be written qualitatively as follows, for m≥1 (equation 2a), and m≤1 (equation 2b):\| (2a) (m-1)MgO + R2MgSiO4 ⇒ (m-1)Mg(OH)2 + "M-S-H" + 2R+ + (OH-, H2SiO4=, CO3=)\| (2b) (1-m)R2SiO3 + mR2MgSiO4 ⇒ "M-S-H" + 2R+ + (OH-, H2SiO4=, CO3=)\|[0045] In the above reactions, the main solid compounds produced are an amorphous magnesium silicate hydrate, "M-S-H", of variable composition, plus, in the case where m>1, magnesium hydroxide (brucite). The alkali metals may dissolve completely in the aqueous phase as alkali metal cations (R+), and the charge of these alkali metal cations is balanced by a mixture of three principal dissolved anions: hydroxide (OH-), silicate (H2SiO4=) and carbonate (CO3=), present in various ratios depending on the conditions and materials used. It is to be understood that equations 2(a) and 2(b) are not perfectly balanced equations but rather are simply intended to indicate the main initial products of the reaction between the solid products of the process of the invention with water.\|[0046] In a further embodiment of the invention the alkaline solution produced in step (d) is contacted with a carbon dioxide-containing gas, for example combustion exhaust gases, to absorb carbon dioxide and yield an alkali metal carbonate, alkali metal bicarbonate or a mixture thereof, generally in solution, and (precipitated) silica.\|[0047] For example, the aqueous solution from step (d) comprising mainly alkali metal hydroxides and silicates and also some residual alkali metal carbonates is contacted with a carbon dioxide-containing gas, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. The solution rapidly absorbs CO2 from such gases to produce a solution of alkali metal carbonates and bicarbonates, and a precipitate of amorphous silica, according to the following, or similar, equations:\| (3) CO2 (gas) + 2ROH (in solution) ⇒ R2CO3 (in solution)\| (4) CO2(gas) + R2SiO3 (in solution) ⇒ R2CO3 (in solution) + SiO2 (solid precipitate)\| (5) CO2 (gas) + R2CO3 (in solution) ⇒ 2RHCO3 (in solution)\|[0048] The resulting solid silica precipitate is separated from the solution, for example by filtering, passage through a hydrocyclone, settling and/or centrifuging. In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled. Additional solutes, e.g. known salts, may also be incorporated into the solution. The precipitated silica formed by reaction (4) above can be separated, washed and dried for use in various applications.\|[0049] It will be understood by mass balance that reactions (3) and (4) should in principle be able to absorb essentially all of the CO2 released by the chemical reaction occurring in the process of the invention as shown in reaction (1), but that the additional CO2 resulting from the combustion process required to heat the starting materials will require an additional reaction to absorb it completely, e.g. either a reaction such as (5), or a further reaction with another absorbent.\|[0050] Magnesium hydroxide produced by the hydration of magnesium oxide prepared by the process of the invention also constitutes a feature of the invention. According to a further feature of the invention the magnesium hydroxide (preferably purified, for example by washing and drying) is calcined to produce magnesium oxide. It will be understood that the value of the magnesium hydroxide or magnesium oxide thus produced will depend mainly on the extent to which the major impurities (in this case, silica, iron compounds and alkali metal salts) are still present, which will be determined by the extent to which they are purified in additional steps such as washing and/or magnetic separation.\|[0051] In a further embodiment of the invention, the magnesium oxide, or magnesium hydroxide produced by the hydration of magnesium oxide, is contacted with a carbon dioxide-containing gas, preferably in the presence of water, to form a magnesium carbonate compound. The rate of this reaction can be controlled by the temperature, the pressure, the relative humidity, the presence of catalysts and/or the type of reactor used. The carbonation reaction is represented by the reaction:\| (6) CO2 (gas) + MgO or Mg(OH)2 ⇒ MgCO3 (solid, possibly hydrated)\|[0052] The products of this carbonation reaction may be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or complex magnesium hydroxy-carbonate hydrates, such as hydromagnesite (Mg(OH)2•4MgCO3•4H2O), or artinite (Mg(OH)2•MgCO3•3H2O), depending on the conditions employed.\|[0053] In a further embodiment of the invention the coarse, partially reacted solids separated from the reaction products in step 1(b) above comprise mainly unreacted magnesium silicate (for example, Mg2SiO4) mixed with some intermediate products (for example, Na2MgSiO4). These can be dried and recycled to be mixed with additional raw magnesium silicate starting material for feeding back into the process. It will be understood that drying should be accomplished in an energy-efficient manner, e.g. first by drainage and then by use of waste heat from the furnace or other sources.\|[0054] According to a further feature of the invention all of the solid products from the process of the invention, e.g. from the furnace or kiln (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4 and MgO and/or QO, and possibly some residual R2CO3 are ground together with water to produce a suspension or slurry which is then contacted with a gas containing carbon dioxide, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. During this treatment, in addition to the other reactions described above, (e.g. in equations (2), (3), (4), (5) and (6)), the alkali magnesium metal orthosilicate compound can also react directly with CO2 as indicated by equations (7) and (8) below:\| (7) R2MgSiO4 + 2CO2 ⇒ MgCO3 (solid) + SiO2 (solid) + R2CO3 (in solution)\|or, alternatively, making use of an alkali bicarbonate solution to achieve the same reaction:\| (8) R2MgSiO4 + 4RHCO3 ⇒ MgCO3 (solid) + SiO2 (solid) + 3R2CO3 (in solution)\|[0055] The alkali metal bicarbonate RHCO3 used in reaction (8) may be formed by the reaction of alkali metal carbonate solution R2CO3 produced in reaction (7) with carbon dioxide, as shown in equation (5).\|[0056] Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300°C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eiteleite, Na2CO3•MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|[0057] These types of reaction are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid products. The magnesium carbonate solid produced can be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or a complex magnesium hydroxy-carbonate hydrate, such as hydromagnesite (Mg(OH)2•4MgCO3•4H2O), or artinite (Mg(OH)2•MgCO3•3H2O), depending on the conditions and starting materials. The silica solid produced can be either a simple amorphous silica or a more complex mixed metal hydroxy-silicate such as a magnesium silicate hydrate ("M-S-H"). The alkali metal carbonate or bicarbonate solutions resulting from complete carbonation as shown in reactions (3), (4), (5), (7) and (8) can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and then recycled to the start of the process. The solid mixture of magnesium carbonates and silica produced by these reactions is one of the final products of the overall process and, after washing if necessary to recover as much as possible of the soluble alkali metal salts, can be separated for disposal or for use in other processes.\|[0058] The overall object of the process is to convert magnesium silicate rock into useful industrial products with low overall CO2 emissions. A further benefit of the process is to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable mineral carbonate which comprises a magnesium carbonate compound. Below are some examples of some different ways in which the process can be used:\| Starting with a magnesium silicate rock of composition m(MgO)•t(QO)•SiO2•xH2O, and recycling substantially all of the alkali metal (R) compounds used back into the process, at least two separate major product streams can be secured from amongst the following:(i) Products rich in magnesium oxide or hydroxide (MgO or Mg(OH)2)\| (ii) Products rich in amorphous silica (SiO2)\| (iii) Products rich in amorphous magnesium silicate hydrates (M-S-H)\| (iv) Products rich in magnesium carbonate compounds, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3 also known as magnesite); or magnesium carbonate trihydrate (MgCO3•3H2O, also known as nesquehonite); or magnesium hydroxy-carbonate hydrate, such as (Mg(OH)2•4MgCO3•4H2O), also known as hydromagnesite, or (Mg(OH)2•MgCO3•3H2O), also known as artinite.\|[0059] Improved separation of the above major solid product streams can also be achieved by the application of other known mineral separation techniques such as, for example, flotation. Such flotation techniques can be effected using flotation aids including sodium oleate, carboxymethylcellulose and methyl isobutyl carbinol.\|[0060] To the extent that CO2 is produced by the combustion of fuels used in the process, e.g. to heat the kiln or furnace, or to dry materials, this CO2 can be captured in the process in the form of product (iv) listed above, by using a treatment process based on the reactions shown above. To the extent that the process is energy-efficient, the aforesaid CO2 produced by the combustion of fuels used in the process, even if substantially completely captured by reactions of the sort shown, for example, in equations (3), (4) and (5), will generally not be sufficient to convert all of the magnesium in the process to product stream (iv), leaving some of the magnesium available for the production of product streams (i) and (iii). However, in another embodiment of the process, additional CO2 can be obtained from other sources and included in the treatment process and thus captured. In such a case, it is possible to operate the process in such a way that product stream (i) is not produced, but the process itself becomes a net consumer of CO2. Moreover, it is also possible to operate the process without separating any of the product streams, so that the only product stream produced is a mixture of some or all of the above product streams\|[0061] In a further approach, (not according to the invention), the process uses the same magnesium silicate raw material as shown above, but in this case, not all of the alkali metal-rich products of the process are recycled within the process. It is therefore possible to have one or more additional product streams as well as those already listed above. For example, one very useful product stream is an alkali metal silicate, (R2SiO3) either in the form of an alkaline aqueous solution also containing alkali metal hydroxides and/or carbonates, or as a solid product, (for example, obtained by evaporation and/or crystallization).\|[0062] According to a feature of the invention the first product is contacted with water to produce a second product comprising magnesium hydroxide which process further comprises (i) carbonation of the second product to produce a carbonated third product and (ii) partial dehydration of the carbonated third product to produce a fourth product.\|[0063] According to a further feature of the invention the first product is contacted with water to produce a second product comprising magnesium hydroxide which process further comprises (i) carbonation of the second product to produce a third product comprising magnesium hydroxide and an alkali metal carbonate and (ii) calcining the magnesium hydroxide from the third product to produce a fifth product comprising magnesium oxide.\|[0064] A hydraulic binder, for example as described in WO2009/156740 A1, comprises the fourth product. The hydraulic binder may further comprise an alkali metal carbonate from the third product. The hydraulic binder may further comprise magnesium oxide from the fifth product.\|[0065] The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|[0066] Another useful product stream is rich in transition metal oxides, for example iron oxides such as magnetite (Fe3O4 and which may also contain significant amounts of chromium and/or nickel oxides. These oxides can be concentrated by flotation and/or magnetic separation.\|[0067] Another useful product stream is an alkaline solution containing chromates, which can be treated with a reducing agent and pH control (or by electrochemical reduction) to separate relatively pure chromium oxides, or even chromium metal; for example:\| R2CrO4(aqueous solution) + (reducing agent) ⇒ Cr(OH)3 (solid precipitate)\|[0068] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0069] The term "pellets" as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0070] Particle size distribution when measured by laser granulometry is measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He-Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.\|[0071] The apparatus is checked before each working session by means of a standard sample (Sifraco C10 silica) for which the particle size distribution is known.\|[0072] Measurements are performed with the following parameters: pump speed 2300rpm and stirrer speed 800rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30s (for possible air bubbles to clear), a measurement is carried out for 15 s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0073] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0074] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R,Q, m, t, x and, p are as initially defined.\|[0075] The following non-limiting Examples illustrate embodiments of the invention.\|[0076] The following abbreviations and notations are used:\|XRF X-ray fluorescence\|XRD X-ray diffraction\|ICP Inductively-Coupled Plasma Photometry\|Hydromagnesite Mg(OH)2•4MgCO3•4H2O\|Artinite Mg(OH)2•MgCO3•3H2O\|Eitelite Na2CO3•Mg(CO3)\|LOI Loss on ignition\|EXAMPLE 1\|[0077] Ground pure olivine sand (Mg0.94Fe0.06)2SiO4 was mixed with sodium carbonate hydrate powder in a 14:11 mass ratio. The molar ratio of this mixture is close to 1:1. 25g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800°C over 2 hours, maintained at 800°C for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table.\|TABLE 1\|SampleLoss on IgnitionSodium carbonate powder14.97 %Ground olivine sand0.22 %14:11 mix of ground olivine sand + sodium carbonate powder16.69 %\|[0078] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by XRD. The reaction products observed by this technique were Na2MgSiO4, MgO and Fe2O3 together with some unreacted olivine and sodium carbonate.\|[0079] 10g of the reacted sample was put into 100 ml of de-ionised water under constant stirring at 40°C for 1h in order to evaluate its dissolution behaviour. The solution was filtered and the solid residue was analysed by XRD. The amounts of dissolved elements in the aqueous solutions were measured by ICP.\|[0080] The main solid phases detected in the filtered solid residue were Na2MgSiO4 MgO, Fe2O3 and olivine. All non-reacted sodium carbonate dissolved in the aqueous solution. Additionally, some dissolved SiO2 was detected with a concentration of 667 mg/l. From this value, one can estimate that 2 to 3% of the total silica from the mixture dissolved in the water under these conditions, (presumed to be as a sodium silicate, as the pH of the solution was measured to be about 12).\|EXAMPLE 2\|[0081] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. The molar ratio of this mixture is approximately 1:1. The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900°C. The sample was air-quenched after 1 h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851 °C). The measured loss on ignition of all of the samples is presented in the following Table.\|TABLE 2\|SampleLoss on IgnitionSodium carbonate14.96 %Olivine0.04 %Olivine + Sodium carbonate23.02 %\|[0082] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by XRD and the phases detected were Na2MgSiO4, MgO, NaFeO2 together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data. The MgO to Na2MgSiO4 mass ratio was estimated by Rietveld analysis of the XRD data to be 14:86, in reasonable agreement with mass balance calculations.\|EXAMPLE 3\|[0083] 13g of the powdered product of Example 2 was mixed with 260 ml of water to give a slurry with about 50g/L solids concentration. This slurry was put in a closed pressure reactor with a total volume of 2 litres, maintained at 25°C. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas and the pH of the aqueous solution were recorded as functions of time and are presented in Figure 2. The rate of pressure drop indicates that the slurry captures gaseous CO2 rapidly, and, concurrently, the pH of the solution falls rapidly from an initial value of over 12 to a final value of about 8.5, consistent with the formation of a mixed sodium carbonate/bicarbonate solution. After this reaction the solids in the slurry were filtered and analysed by XRD. NaFeO2 was no longer detectable and the MgO:Na2MgSiO4 ratio had increased to an estimated value of 18:82, indicating that some sodium silicate had leached out of the Na2MgSiO4 phase into the solution and had then been carbonated.\|EXAMPLE 4\|[0084] 5g of the powdered product of Example 2 was mixed with 200 ml of water to give a slurry of about 25g/L solids concentration. This slurry was then boiled gently for one hour, after which it was filtered and the solid residue analyzed by XRD. The relative concentration of the Na2MgSiO4 phase in the residue was clearly greatly reduced compared to the original untreated residue, and the relative concentration of MgO greatly increased. The NaFeO2 phase had also completely disappeared but peaks for a layered double hydroxide phase probably having a formula close to 4MgO•Fe2O3•CO2•10H2O were seen clearly, together with weaker peaks for Fe2O3 (haematite) and unreacted olivine.\|[0085] The liquid filtrate was also analyzed by ICP and the results (see the Table below) showed a high concentration (6.92 g/L as Na2O) of sodium in solution, as well as 0.47 g/L of SiO2. This confirms that most of the sodium had leached out of the sample, and that about 15% of it was probably in the form of a sodium metasilicate solution, the rest presumed to be a mixture of sodium hydroxide and sodium carbonate.\|Chemical analysis of the aqueous solution\|TABLE 3\|[0086] Chemical speciesConcentration [mg/l]SiO2466Al2O36.65Fe2O31.78CaO0.51MgO1.51K2O2.40Na2O6920SO32.53P0.58\|EXAMPLE 5\|[0087] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 litres, maintained at 35°C and agitated with a mechanical stirrer operating at 500rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its absorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in the following Table.\|TABLE 4\|Experiment n°Total CO2 captured (mol)Slurry volume (mL)Slurry conc. (g/L)Total solids. (g)CO2 captured, as % of theoretical maximumSlurry additivesTemp. (°C)Duration (h)Solid products detected10.06412605013.035Na2CO3: 21.15 g/L3524Hydromagne site20.07242605013.040Na2CO3: 53.85 g/L3524Hydromagne site30.13632605013.075NaHCO3: 53.85 g/L3530Hydromagne site40.035226011.52.99843526Artinite\|[0088] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite and, in one case, artinite, which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 6\|[0089] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometre sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950°C), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio (molar ratio approximately 1:1.3). About 5kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950°C for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by XRF spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3 and 33.4% sodium expressed as Na2O. An XRD analysis showed the major phases present in the product to be Na2MgSiO4 and periclase (MgO).\|EXAMPLE 7\|[0090] The reaction products of Example 2 (referred to hereinafter as "product X") and of Example 6 (referred to hereinafter as "product XS") were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75g of the solid were added to 1.5 litres of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal litres per hour at close to one atmosphere absolute pressure. The reactor contents were maintained at 70°C by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements by ICP. The solid filter-cakes were dried at 110°C and then analysed by XRF spectrometry for elemental composition, by XRD for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0091] The results for three different product samples are given in the following Table\|TABLE 5\|Experiment N° ; anhydrous product usedDuration (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %5 Product X3.5420Hydromagnesite31.215.918.20.65961 Product X4.0600Hydromagnesite30.316.418.80.5637 Product XS4.0205Hydromagnesite27.717.219.70.471(1) In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0092] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields of the order of 60-70% of the total magnesium in the starting material in about 3.5 to 4 hours. Based on XRF analyses of the solid phases coupled with ICP analyses of the liquid phase, it is estimated that roughly 90% of the initial Na and 50% of the initial Cr in the product leached out during the experiment.\|EXAMPLE 8\|Formation of eitelite.\|[0093] The procedure of Example 7 was repeated using two slurries (prepared from products X and XS from Examples 2 and 6, respectively) at a concentration of 150g/L, i.e. three times the concentration used in Example 7.\|[0094] During the 3 first hours the same trends were observed as those in Example 7. But after 4 hours, XRD revealed the presence of eitelite as well as hydromagnesite. The results are given in the following Table.\|TABLE 6\|Experiment N° ; anhydrous product usedDuratio n (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %8 Product X4.0600Hydromagnesite & eitelite28.0616.4518.830.567.129 Product XS4.0600Hydromagnesite & eitelite25.7415.8218.110.870.37\|EXAMPLE 9\|Effectiveness of water leaching\|[0095] 50g of product X was washed in 1 L deionised water 6 times in series (15minutes stirring in between at room temperature and atmospheric pressure, i.e. 25°C and 1 bar). Each time a small sample was taken to analyse the solids and the liquids. The XRF results for product X coupled with ICP solution analyses lead to the results given in the following Table, which the percentages of each element leached from the product are given as a function of the number of washing steps.\|TABLE 7\|% leachedSiCaMgKNaSCrWashing 19.850.460.0019.7636.4413.7746.12Washing 23.200.090.001.948.690.601.30Washing 31.410.020.000.253.470.040.21Washing 41.220.020.000.033.530.130.32Washing 50.750.020.000.021.870.140.12Washing 60.510.050.000.001.300.050.08TOTAL16.940.660.0122.0055.3114.7348.15\|[0096] The first washing step was clearly the most efficient. Therefore 500g of product X were washed in the same conditions, the solid was then filtered and dried overnight at 110°C. Finally the same carbonation experiment as described in Example 8 was performed on this solid product. This time XRD analysis revealed only hydromagnesite; no eitelite was detected. This shows that washing can be used to enhance Na recycling in the process.\|[0097] The analysis of the solution obtained after the first washing (table below) showed it to have a high pH and to contain about 4000mg/L of Na and 637 mg/L of Si, the other elements being present in much smaller amounts. On this basis, the solution was estimated to contain about 23 milimoles/litre of sodium metasilicate (Na2SiO3 and 130 millimoles/litre of sodium hydroxide (NaOH), possibly also including some carbonate ions.\|TABLE 8\|In mg/l (elements)SiCaMgKNaSCrWashing 1637.50.2990.2674.140001.38\|EXAMPLE 10\|Hydromagnesite formation at 60°C\|[0098] 1 L of a 50g/L slurry of product X was prepared and poured into a 2L autoclave. The system was closed and 1 L of pure CO2 at 10 bars was added without purging the residual air, after which the slurry was stirred and heated up to 60°C (which roughly corresponds to the dew point of exhaust gases in a cement plant). After 2 hours the pressure dropped to close to atmospheric and heating of the autoclave was stopped. The next day, the slurry was filtered and dried overnight at 110°C. XRD revealed hydromagnesite as the main crystalline product.\|EXAMPLE 11\|Formation of magnesite as main product at 120°C.\|[0099] The procedure of Example 10 was repeated but at 120°C (a typical temperature for exhaust gases from a cement plant) using the same autoclave, and adding CO2 each time the pressure dropped close to two bars (the equilibrium water vapour pressure at 120°C). Three additions of CO2 up to 10 bars were made in the space of one day. XRD on the dried solid revealed magnesite (MgCO3 to be the main product, but also showed some traces of magnetite (Fe3O4). ICP analysis of the aqueous phase showed 90% leaching of Na. The combined CO2 content in the solids was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser and showed that the amount of MgCO3 present accounted for about 47% of the original Mg in Product X.\|EXAMPLE 12\|Selective separation of chromium by reduction in solution.\|[0100] Powdered product X was stirred with deionised water for 15 minutes at a 2:1 water:solids mass ratio. The yellow-coloured aqueous phase was filtered and a sample taken for ICP analysis. Excess ferrous sulfate (FeSO4), a reducing agent, was then added in powder form to the solution, after which a chromium-containing precipitate formed. The liquid was again filtered, giving a colourless solution which was again analysed by ICP. The chromium content of the yellow-coloured aqueous phase was 772 mg/L. The colourless solution contained only 29 mg/L of chromium.\|[0101] These results, when compared with the analysis of the raw materials, indicated that about 50% of the total chromium in the original raw material (olivine) was converted into a readily soluble (chromate) form by the process used to make "product X," and 96% of the Cr leached into the solution was precipitated by addition of ferrous sulfate.\|EXAMPLE 13\|Concentration of hydromagnesite from the solid residues by flotation\|[0102] Separation tests were performed by flotation on the carbonated products produced from the application of the process to olivine and serpentine, similarl to the products shown, respectively, for experiments 5 and 7 in the table of Example 7. Combinations of sodium oleate, carboxymethylcellulose (CMC) and methyl isobutyl carbinol (MIBC) were used in the aqueous phase sequentially to disperse the solids in the form of a slurry at a solids concentration of 90g/L.\|[0103] First sodium oleate was added to the slurry and stirred for 5 minutes in a beaker in order to render carbonated particles hydrophobic. Then CMC was added to depress silicate hydrophobicity, followed by a further 5 minutes of stirring; and finally MIBC was added in order to stabilise the foam formed by air bubbling.\|[0104] Air was bubbled through the treated slurry in a miniature flotation cell, and the solids carried over by the foam were collected as "concentrate." The residual solids were collected as "tailings." Results of four such experiments are presented in the table below. The CO2 content was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser. The CO2 contents of the concentrates were typically 3-4 times greater than those of the tailings, showing that hydromagnesite can be effectively separated by flotation in this manner.\|[0105] The XRD results confirm the separation. They are expressed in a qualitative way by different symbols expressing the probability of a phase presence:\| (o) not present,\| () possibly present,\| (X) definitely present,\| (X+) present in abundance.\|TABLE 9\|Chemical additive (dosage, ppm)Test 1Test 2Test 3Test 4Sodium oleate1500100020001000CMC200200200200MIBC20202020Product tested by flotation:Carbonated "product X"Carbonate "product X"Carbonated "product X"Carbonated "product XS"Results of flotati on testsTailingsCon centrateTailingsConcentrateTailingsConcentrateTailingsConcentrateComponents measured by chemical analysisSiO2 %34.117.633.718.533.822.033.316.9Fe2O3 %6.43.46.43.66.44.36.93.0MgO %34.637.234.537.233.936.929.235.9Na2O %2.31.32.31.42.61.32.31.2LOI %22.340.022.638.922.735.126.241.6CO2 %5.722.25.820.25.717.39.423.0Phases detected by XRDSodium magnesium silicate00000000PericlaseXXX*OlivineXXX00HydromagnesiteXX+XX+XX+XX+\|EXAMPLE 14\|[0106] (not according to the invention) Ground natural talc from Luzenac (France) with nominal composition Mg3Si4O10(OH)2 and containing some minor impurities (1.1% Al2O3, 0.9 % Fe2O3 and 0.9% CaO by mass) was mixed with anhydrous sodium carbonate (Na2CO3) at a 4863:5136 mass ratio (molar ratio approximately 1:1). The composition was chosen in order to obtain an atomic ratio of 2:1 Na:Si in the final sample. 20.5g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. The sample was heated at 900°C for 1 hour, followed by cooling in air. It was weighed before and after treatment and the measured loss on ignition of 23.3% was consistent with evaporation of carbon dioxide from the sodium carbonate plus bound water from the talc; it represents about 95% of the theoretical value for complete reaction of 24.6%. The phase constitution of the reacted sample was determined by X-ray diffraction: the main products detected were Na2MgSiO4 and Na2SiO3.	(EP2735553)\|[0001] This invention relates to a process for the treatment of a silicate mineral, The process uses as starting material a magnesium silicate and produces an alkali metal magnesium orthosilicate and magnesium oxide each of which can be isolated or subjected to further treatment to produce other products.\|[0002] US5085838 discloses preparation of a product comprising an alkali metal magnesium orthosilicate and a magnesium oxide, in which an alkali metal carbonate compound is reacted with a magnesium silicate.\|[0003] US2012291675 and US2004213705 describe processes for the sequestration of CO2 WO20070159902 discloses a method for industrial manufacture of pure MgCO3 from an olivine containing species of rock.\|[0004] XP2994928 describes a process where sodium bicarbonate, sodium chloride and water are mixed with magnesium silicates.\|[0005] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into common magnesium silicate hydrate minerals such as serpentine (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10(OH)2). Magnesium silicate rocks constitute an excellent source of two important elements, magnesium and silicon, in their oxide forms (MgO and SiO2). Processes to extract these two oxides from such rocks have heretofore been excessively energy-intensive and thus have not been commercialized.\|[0006] Although the magnesium silicate minerals tend to be very "unreactive," (e,g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a "carbonate fusion", is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analyzed by standard chemical techniques, thus allowing for total elemental analysis of the rock The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0007] The term sodium magnesium silicate is sometimes used, in accordance with the International Nomenclature of Cosmetic Ingredients (INCI) to identify synthetic hectorites in the form of nanoparticles and which form clear gels in water According to one manufacturer of such products hectorites have the formula (Mg5.2Li0.8)(Si8)O20(OH)4Na0.8.\|[0008] The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|[0009] The present invention accordingly provides a process for the treatment of a silicate mineral comprising a first step of preparation of a first product comprising an alkali metal magnesium orthosilicate of the general formula R2MgSiO4 wherein R represents an alkali metal, and magnesium oxide which process comprises the reaction, at a temperature from 500 to 200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, a second step of contacting the first product with water to produce a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate, and a third step of isolating or producing magnesium oxide, magnesium hydroxide from the second product.\|[0010] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate, expressed as silicon dioxide, is preferably from <4:1 to 1:4, more preferably from 3:1 to 1:3, for example 2:1 to 1:2. The ratio is most preferably about 1.\|[0011] The alkali metal is preferably potassium or, more preferably, sodium.\|[0012] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used in the process of the invention.\|[0013] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0014] The magnesium silicate used in the process of the invention is generally a mineral silicate, for example a rock comprising a high concentration, preferably 20% or more, more preferably 50% or more, of a magnesium silicate of general composition:\| m(MgO)•t(QO)•SiO3•xH2O\|wherein m is from 1 to 3, t is less than or equal to 1, and x is from zero to 2: and Q represents a metal or metals other than magnesium, (for example calcium and/or a transition group metal such as iron, chromium or nickel). It will be understood that the composition or formulae of minerals is often depicted in terms of the theoretical amount of oxides which they contain: the oxides are, however, not present as such in the minerals whose composition is depicted in this way.\|[0015] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc, iddingsite and hectorite. These minerals may contain substantial quantities of iron in addition to magnesium and silicon, and also significant amounts of calcium, aluminium and alkali metals,\|[0016] Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, arlthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0017] The mineral silicate used in the process of the invention is preferably a magnesium silicate. The MgO/SiO2 molar ratio is 1-3. The CaO/SiO2 molar ratio is preferably ≤0.5. The FeO/SiO2 molar ratio is preferably ≤0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≤0.2.\|[0018] The alkali metal carbonate compound used in the process of the invention may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2•2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g chlorides, sulfates, sulphites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates or hydroxides) are present which, at the temperature used in the process of the invention, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0019] The process of the invention is preferably effected at a temperature from 600 to 1100°C, more preferably from 800 to 1000°C. Heating is generally effected for a few minutes to a few hours.\|[0020] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is solid or liquid.\|[0021] According to a feature of the invention the process is effected at a temperature below the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound.\|[0022] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as "R2O" in which R is as hereinbefore defined present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt. = 140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt. = 106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0023] The magnesium silicate and alkali metal carbonate compound used in the process of the present invention are preferably in particulate form or in shaped form, e.g. as pellets.\|[0024] Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the process of the invention will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of a fine sand (grain size 0.06 to 0.2mm) or, if necessary, ground to a fine powder (grain sizes below 0.06mm). Grain sizes greater than 0.06mm are generally determined by sieving. Grain sizes lower than 0.06mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0025] In one embodiment the process of the invention is conducted in a moving grate furnace. This procedure is especially suited to magnesium silicate rocks (rocks comprising mainly MgO and SiO2) in which the MgO/SiO2 molar ratio is close to or greater than 1.\|[0026] A mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in Figure 1 of the accompanying drawings.\|[0027] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0028] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone ("burning zone") just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1a) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate (R2CO3)\| (1a) Mg2SiO4 + R2CO3 ⇒ MgO + R2MgSiO4 + CO2↑\|in which R is as hereinbefore defined. The more general form of this reaction can be written as in equation (1 b) for m>=1 and equation 1 (c) for m<1:\| (1b) m(MgO)•t(QO)•SiO2•xH2O + R2CO3 ⇒ (m-1)MgO + R2MgSiO4 + tQO + CO2↑ + xH2O↑\| (1c) m(MgO)•t(QO)•SiO2•xH2O + R2CO3 ⇒ (1-m)R2SiO3 + mR2MgSiO4 + tQO + CO2↑ + xH2O↑\|wherein m is greater than or equal to 1 for reaction (1 b) and less than or equal to 1 for reaction (1 c); and Q, t and x are as hereinbefore defined. The vertical arrows T indicate that the carbon dioxide gas and water vapour produced by this reaction escape from the bed and exits with the rest of the exhaust gases. Thus, ideally, the final solid product remaining in the treated pellets is an intimate mixture comprising magnesium oxide (MgO also known as periclase) and alkali metal magnesium orthosilicate (R2MgSiO4) and/or alkali metal silicates (R2SiO3) as well as other solid products comprising the other metals (Q), especially iron, which may present as magnetite (Fe3O4) or possibly as an alkali metal ferrite (RFeO2), calcium, which may be present as silicates, chromium, which may be present as alkali metal chromates (R2CrO4), and nickel, which may be present as oxides.\|[0029] The idealized reactions depicted in equations (1 a,b,c) illustrate the production of alkali metal magnesium orthosilicates plus magnesium and/or other oxides and silicates by direct reaction of a stoichiometric (i.e. 1:1 R2O:SiO2) mixture of a magnesium silicate and an alkali metal carbonate.\|[0030] This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 3.4 kJ (i.e. about 0.8 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, there will be a significant net energy consumption for the overall process. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0031] In a further embodiment, the process of the invention is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln for the process of the invention which comprises a decarbonation step which produces carbon dioxide.\|[0032] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0033] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 35% of the total solids volume. However, since the reaction itself produces no liquid products (only solids and gases) at the temperatures preferably employed, the risk of the nodules deforming significantly due to melting is quite low even at far higher initial volume fractions of alkali metal carbonate as long as the heating occurs slowly enough to allow for a significant degree of reaction to occur before complete melting of the alkali metal carbonate.\|[0034] According to a further feature of the invention the process of the invention is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The nodules are then decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0035] The decarbonated and cooled pellets or nodules, comprising alkali metal magnesium orthosilicate and magnesium oxide or alkali metal silicate, are treated in order to separate the reaction products.\|[0036] In the process of the invention the first product comprising alkali metal magnesium orthosilicate and magnesium oxide is contacted with water to form a second product by hydrating the magnesium oxide to magnesium hydroxide and to partially dissolve the alkali metal magnesium orthosilicate.\|[0037] The first product as, for example pellets or nodules, is preferably quenched in an amount of water, such that the final mixture after quenching has a temperature close to, but not exceeding, about 100°C, i.e. enough to quench the solids but avoiding excessive evaporation of water. The hot quenched solids are then preferably crushed and agitated mechanically in the form of a slurry. More water may be added if necessary. Some additional heating may be necessary.\|[0038] Alternatively the treatment with water, for example in the quenching and slurry-formation process described above, can be conducted at a temperature above 100°C if a pressurized vessel (e.g. an autoclave) is used.\|[0039] Alternatively the above quenching and slurry-formation process can be conducted at lower or ambient temperatures. Water for converting the first product into the second product can optionally be recycled from another part of the process.\|[0040] The objective is to separate the components of the second product by virtue of the facts that (a) alkali metal carbonates, silicates, chromates, sulfates and oxides or hydroxides in the product will tend to dissolve readily in water; (b) alkali metal magnesium orthosilicates will tend to hydrate in hot water to release alkali metals into solution as silicates and hydroxides, the remainder giving a fine suspension of solid magnesium silicate hydrates, and (c) magnesium oxide (MgO, also known as periclase) in the sample will tend to hydrate in hot water to give magnesium hydroxide (Mg(OH)2, also known as brucite) to form a soft and easily-dispersible powder.\|[0041] The slurry may need to be agitated mechanically. Then, the liquid phase can be separated from the bulk of the unreacted alkali metal magnesium orthosilicate and other unreacted anhydrous compounds, for example by sieving, and the fine particles of magnesium hydroxide and/or magnesium silicate hydrates which pass through the sieve as a slurry may be separated from the slurry by, for example, filtering, passage through a hydrocyclone, settling and/or centrifuging. The aqueous phase after separation of the magnesium hydroxide comprises an aqueous solution of alkali metal silicates and hydroxides.\|[0042] Alternatively, the separation process may be conducted in two steps, the first step comprising a rapid washing process to remove most of the readily soluble alkali metal carbonates, silicates and hydroxides; and the second step, conducted with additional water, comprising further hydration of both the magnesium oxide and the alkali metal magnesium orthosilicate. In this two-step approach, the water temperature is preferably lower for the first step (for example lower than 60°C) than for the second step, and an autoclave may be used for the second step if necessary.\|[0043] The overall result of the separation process described above can be summarized as follows: Solid products from the process of the invention, e.g. from the furnace or kiln, (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4, MgO or R2SiO3, QO, and possibly some residual R2CO3) are contacted with water to produce a second product comprising:\| (a) a fine suspension comprising Mg(OH)2 and/or magnesium silicate hydrates in a highly alkaline solution rich in alkali metal silicates, hydroxides and carbonates, and\| (b) coarse unreacted solids comprising R2MgSiO4, MgO, QO and unreacted particles of the original magnesium silicate rock (e.g. Mg2SiO4), and which separate easily by sedimentation (e.g. in a hydrocyclone) from the fine suspension.\|The fine suspension can then be further separated (e.g. by filtration) to give\| (c) fine solids rich in Mg(OH)2 and/or magnesium silicate hydrates, and\| (d) a solution rich in alkali metal silicates, hydroxides and carbonates, and also comprising minor amounts of alkali-soluble impurities, e.g. sulfates and chromates.\|[0044] The initial part of the reaction of the solid products in the process with water can be written qualitatively as follows, for m≥1 (equation 2a), and m≤1 (equation 2b):\| (2a) (m-1)MgO + R2MgSiO4 ⇒ (m-1)Mg(OH)2 + "M-S-H" + 2R+ + (OH-, H2SiO4=, CO3=)\| (2b) (1-m)R2SiO3 + mR2MgSiO4 ⇒ "M-S-H" + 2R+ + (OH-, H2SiO4=, CO3=)\|[0045] In the above reactions, the main solid compounds produced are an amorphous magnesium silicate hydrate, "M-S-H", of variable composition, plus, in the case where m>1, magnesium hydroxide (brucite). The alkali metals may dissolve completely in the aqueous phase as alkali metal cations (R+), and the charge of these alkali metal cations is balanced by a mixture of three principal dissolved anions: hydroxide (OH-), silicate (H2SiO4=) and carbonate (CO3=), present in various ratios depending on the conditions and materials used. It is to be understood that equations 2(a) and 2(b) are not perfectly balanced equations but rather are simply intended to indicate the main initial products of the reaction between the solid products of the process of the invention with water.\|[0046] In a further embodiment of the invention the alkaline solution produced in step (d) is contacted with a carbon dioxide-containing gas, for example combustion exhaust gases, to absorb carbon dioxide and yield an alkali metal carbonate, alkali metal bicarbonate or a mixture thereof, generally in solution, and (precipitated) silica.\|[0047] For example, the aqueous solution from step (d) comprising mainly alkali metal hydroxides and silicates and also some residual alkali metal carbonates is contacted with a carbon dioxide-containing gas, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. The solution rapidly absorbs CO2 from such gases to produce a solution of alkali metal carbonates and bicarbonates, and a precipitate of amorphous silica, according to the following, or similar, equations:\| (3) CO2 (gas) + 2ROH (in solution) ⇒ R2CO3 (in solution)\| (4) CO2(gas) + R2SiO3 (in solution) ⇒ R2CO3 (in solution) + SiO2 (solid precipitate)\| (5) CO2 (gas) + R2CO3 (in solution) ⇒ 2RHCO3 (in solution)\|[0048] The resulting solid silica precipitate is separated from the solution, for example by filtering, passage through a hydrocyclone, settling and/or centrifuging. In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled. Additional solutes, e.g. known salts, may also be incorporated into the solution. The precipitated silica formed by reaction (4) above can be separated, washed and dried for use in various applications.\|[0049] It will be understood by mass balance that reactions (3) and (4) should in principle be able to absorb essentially all of the CO2 released by the chemical reaction occurring in the process of the invention as shown in reaction (1), but that the additional CO2 resulting from the combustion process required to heat the starting materials will require an additional reaction to absorb it completely, e.g. either a reaction such as (5), or a further reaction with another absorbent.\|[0050] Magnesium hydroxide produced by the hydration of magnesium oxide prepared by the process of the invention also constitutes a feature of the invention. According to a further feature of the invention the magnesium hydroxide (preferably purified, for example by washing and drying) is calcined to produce magnesium oxide. It will be understood that the value of the magnesium hydroxide or magnesium oxide thus produced will depend mainly on the extent to which the major impurities (in this case, silica, iron compounds and alkali metal salts) are still present, which will be determined by the extent to which they are purified in additional steps such as washing and/or magnetic separation.\|[0051] In a further embodiment of the invention, the magnesium oxide, or magnesium hydroxide produced by the hydration of magnesium oxide, is contacted with a carbon dioxide-containing gas, preferably in the presence of water, to form a magnesium carbonate compound. The rate of this reaction can be controlled by the temperature, the pressure, the relative humidity, the presence of catalysts and/or the type of reactor used. The carbonation reaction is represented by the reaction:\| (6) CO2 (gas) + MgO or Mg(OH)2 ⇒ MgCO3 (solid, possibly hydrated)\|[0052] The products of this carbonation reaction may be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or complex magnesium hydroxy-carbonate hydrates, such as hydromagnesite (Mg(OH)2•4MgCO3•4H2O), or artinite (Mg(OH)2•MgCO3•3H2O), depending on the conditions employed.\|[0053] In a further embodiment of the invention the coarse, partially reacted solids separated from the reaction products in step 1(b) above comprise mainly unreacted magnesium silicate (for example, Mg2SiO4) mixed with some intermediate products (for example, Na2MgSiO4). These can be dried and recycled to be mixed with additional raw magnesium silicate starting material for feeding back into the process. It will be understood that drying should be accomplished in an energy-efficient manner, e.g. first by drainage and then by use of waste heat from the furnace or other sources.\|[0054] According to a further feature of the invention all of the solid products from the process of the invention, e.g. from the furnace or kiln (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4 and MgO and/or QO, and possibly some residual R2CO3 are ground together with water to produce a suspension or slurry which is then contacted with a gas containing carbon dioxide, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. During this treatment, in addition to the other reactions described above, (e.g. in equations (2), (3), (4), (5) and (6)), the alkali magnesium metal orthosilicate compound can also react directly with CO2 as indicated by equations (7) and (8) below:\| (7) R2MgSiO4 + 2CO2 ⇒ MgCO3 (solid) + SiO2 (solid) + R2CO3 (in solution)\|or, alternatively, making use of an alkali bicarbonate solution to achieve the same reaction:\| (8) R2MgSiO4 + 4RHCO3 ⇒ MgCO3 (solid) + SiO2 (solid) + 3R2CO3 (in solution)\|[0055] The alkali metal bicarbonate RHCO3 used in reaction (8) may be formed by the reaction of alkali metal carbonate solution R2CO3 produced in reaction (7) with carbon dioxide, as shown in equation (5).\|[0056] Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300°C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eiteleite, Na2CO3•MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|[0057] These types of reaction are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid products. The magnesium carbonate solid produced can be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3•3H2O), or a complex magnesium hydroxy-carbonate hydrate, such as hydromagnesite (Mg(OH)2•4MgCO3•4H2O), or artinite (Mg(OH)2•MgCO3•3H2O), depending on the conditions and starting materials. The silica solid produced can be either a simple amorphous silica or a more complex mixed metal hydroxy-silicate such as a magnesium silicate hydrate ("M-S-H"). The alkali metal carbonate or bicarbonate solutions resulting from complete carbonation as shown in reactions (3), (4), (5), (7) and (8) can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and then recycled to the start of the process. The solid mixture of magnesium carbonates and silica produced by these reactions is one of the final products of the overall process and, after washing if necessary to recover as much as possible of the soluble alkali metal salts, can be separated for disposal or for use in other processes.\|[0058] The overall object of the process is to convert magnesium silicate rock into useful industrial products with low overall CO2 emissions. A further benefit of the process is to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable mineral carbonate which comprises a magnesium carbonate compound. Below are some examples of some different ways in which the process can be used:\| Starting with a magnesium silicate rock of composition m(MgO)•t(QO)•SiO2•xH2O, and recycling substantially all of the alkali metal (R) compounds used back into the process, at least two separate major product streams can be secured from amongst the following:(i) Products rich in magnesium oxide or hydroxide (MgO or Mg(OH)2)\| (ii) Products rich in amorphous silica (SiO2)\| (iii) Products rich in amorphous magnesium silicate hydrates (M-S-H)\| (iv) Products rich in magnesium carbonate compounds, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3 also known as magnesite); or magnesium carbonate trihydrate (MgCO3•3H2O, also known as nesquehonite); or magnesium hydroxy-carbonate hydrate, such as (Mg(OH)2•4MgCO3•4H2O), also known as hydromagnesite, or (Mg(OH)2•MgCO3•3H2O), also known as artinite.\|[0059] Improved separation of the above major solid product streams can also be achieved by the application of other known mineral separation techniques such as, for example, flotation. Such flotation techniques can be effected using flotation aids including sodium oleate, carboxymethylcellulose and methyl isobutyl carbinol.\|[0060] To the extent that CO2 is produced by the combustion of fuels used in the process, e.g. to heat the kiln or furnace, or to dry materials, this CO2 can be captured in the process in the form of product (iv) listed above, by using a treatment process based on the reactions shown above. To the extent that the process is energy-efficient, the aforesaid CO2 produced by the combustion of fuels used in the process, even if substantially completely captured by reactions of the sort shown, for example, in equations (3), (4) and (5), will generally not be sufficient to convert all of the magnesium in the process to product stream (iv), leaving some of the magnesium available for the production of product streams (i) and (iii). However, in another embodiment of the process, additional CO2 can be obtained from other sources and included in the treatment process and thus captured. In such a case, it is possible to operate the process in such a way that product stream (i) is not produced, but the process itself becomes a net consumer of CO2. Moreover, it is also possible to operate the process without separating any of the product streams, so that the only product stream produced is a mixture of some or all of the above product streams\|[0061] In a further approach, (not according to the invention), the process uses the same magnesium silicate raw material as shown above, but in this case, not all of the alkali metal-rich products of the process are recycled within the process. It is therefore possible to have one or more additional product streams as well as those already listed above. For example, one very useful product stream is an alkali metal silicate, (R2SiO3) either in the form of an alkaline aqueous solution also containing alkali metal hydroxides and/or carbonates, or as a solid product, (for example, obtained by evaporation and/or crystallization).\|[0062] According to a feature of the invention the first product is contacted with water to produce a second product comprising magnesium hydroxide which process further comprises (i) carbonation of the second product to produce a carbonated third product and (ii) partial dehydration of the carbonated third product to produce a fourth product.\|[0063] According to a further feature of the invention the first product is contacted with water to produce a second product comprising magnesium hydroxide which process further comprises (i) carbonation of the second product to produce a third product comprising magnesium hydroxide and an alkali metal carbonate and (ii) calcining the magnesium hydroxide from the third product to produce a fifth product comprising magnesium oxide.\|[0064] A hydraulic binder, for example as described in WO2009/156740 A1, comprises the fourth product. The hydraulic binder may further comprise an alkali metal carbonate from the third product. The hydraulic binder may further comprise magnesium oxide from the fifth product.\|[0065] The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|[0066] Another useful product stream is rich in transition metal oxides, for example iron oxides such as magnetite (Fe3O4 and which may also contain significant amounts of chromium and/or nickel oxides. These oxides can be concentrated by flotation and/or magnetic separation.\|[0067] Another useful product stream is an alkaline solution containing chromates, which can be treated with a reducing agent and pH control (or by electrochemical reduction) to separate relatively pure chromium oxides, or even chromium metal; for example:\| R2CrO4(aqueous solution) + (reducing agent) ⇒ Cr(OH)3 (solid precipitate)\|[0068] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0069] The term "pellets" as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0070] Particle size distribution when measured by laser granulometry is measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He-Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.\|[0071] The apparatus is checked before each working session by means of a standard sample (Sifraco C10 silica) for which the particle size distribution is known.\|[0072] Measurements are performed with the following parameters: pump speed 2300rpm and stirrer speed 800rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30s (for possible air bubbles to clear), a measurement is carried out for 15 s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0073] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0074] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R,Q, m, t, x and, p are as initially defined.\|[0075] The following non-limiting Examples illustrate embodiments of the invention.\|[0076] The following abbreviations and notations are used:\|XRF X-ray fluorescence\|XRD X-ray diffraction\|ICP Inductively-Coupled Plasma Photometry\|Hydromagnesite Mg(OH)2•4MgCO3•4H2O\|Artinite Mg(OH)2•MgCO3•3H2O\|Eitelite Na2CO3•Mg(CO3)\|LOI Loss on ignition\|EXAMPLE 1\|[0077] Ground pure olivine sand (Mg0.94Fe0.06)2SiO4 was mixed with sodium carbonate hydrate powder in a 14:11 mass ratio. The molar ratio of this mixture is close to 1:1. 25g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800°C over 2 hours, maintained at 800°C for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table.\|TABLE 1\|SampleLoss on IgnitionSodium carbonate powder14.97 %Ground olivine sand0.22 %14:11 mix of ground olivine sand + sodium carbonate powder16.69 %\|[0078] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by XRD. The reaction products observed by this technique were Na2MgSiO4, MgO and Fe2O3 together with some unreacted olivine and sodium carbonate.\|[0079] 10g of the reacted sample was put into 100 ml of de-ionised water under constant stirring at 40°C for 1h in order to evaluate its dissolution behaviour. The solution was filtered and the solid residue was analysed by XRD. The amounts of dissolved elements in the aqueous solutions were measured by ICP.\|[0080] The main solid phases detected in the filtered solid residue were Na2MgSiO4 MgO, Fe2O3 and olivine. All non-reacted sodium carbonate dissolved in the aqueous solution. Additionally, some dissolved SiO2 was detected with a concentration of 667 mg/l. From this value, one can estimate that 2 to 3% of the total silica from the mixture dissolved in the water under these conditions, (presumed to be as a sodium silicate, as the pH of the solution was measured to be about 12).\|EXAMPLE 2\|[0081] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. The molar ratio of this mixture is approximately 1:1. The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900°C. The sample was air-quenched after 1 h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851 °C). The measured loss on ignition of all of the samples is presented in the following Table.\|TABLE 2\|SampleLoss on IgnitionSodium carbonate14.96 %Olivine0.04 %Olivine + Sodium carbonate23.02 %\|[0082] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by XRD and the phases detected were Na2MgSiO4, MgO, NaFeO2 together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data. The MgO to Na2MgSiO4 mass ratio was estimated by Rietveld analysis of the XRD data to be 14:86, in reasonable agreement with mass balance calculations.\|EXAMPLE 3\|[0083] 13g of the powdered product of Example 2 was mixed with 260 ml of water to give a slurry with about 50g/L solids concentration. This slurry was put in a closed pressure reactor with a total volume of 2 litres, maintained at 25°C. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas and the pH of the aqueous solution were recorded as functions of time and are presented in Figure 2. The rate of pressure drop indicates that the slurry captures gaseous CO2 rapidly, and, concurrently, the pH of the solution falls rapidly from an initial value of over 12 to a final value of about 8.5, consistent with the formation of a mixed sodium carbonate/bicarbonate solution. After this reaction the solids in the slurry were filtered and analysed by XRD. NaFeO2 was no longer detectable and the MgO:Na2MgSiO4 ratio had increased to an estimated value of 18:82, indicating that some sodium silicate had leached out of the Na2MgSiO4 phase into the solution and had then been carbonated.\|EXAMPLE 4\|[0084] 5g of the powdered product of Example 2 was mixed with 200 ml of water to give a slurry of about 25g/L solids concentration. This slurry was then boiled gently for one hour, after which it was filtered and the solid residue analyzed by XRD. The relative concentration of the Na2MgSiO4 phase in the residue was clearly greatly reduced compared to the original untreated residue, and the relative concentration of MgO greatly increased. The NaFeO2 phase had also completely disappeared but peaks for a layered double hydroxide phase probably having a formula close to 4MgO•Fe2O3•CO2•10H2O were seen clearly, together with weaker peaks for Fe2O3 (haematite) and unreacted olivine.\|[0085] The liquid filtrate was also analyzed by ICP and the results (see the Table below) showed a high concentration (6.92 g/L as Na2O) of sodium in solution, as well as 0.47 g/L of SiO2. This confirms that most of the sodium had leached out of the sample, and that about 15% of it was probably in the form of a sodium metasilicate solution, the rest presumed to be a mixture of sodium hydroxide and sodium carbonate.\|Chemical analysis of the aqueous solution\|TABLE 3\|[0086] Chemical speciesConcentration [mg/l]SiO2466Al2O36.65Fe2O31.78CaO0.51MgO1.51K2O2.40Na2O6920SO32.53P0.58\|EXAMPLE 5\|[0087] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 litres, maintained at 35°C and agitated with a mechanical stirrer operating at 500rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its absorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in the following Table.\|TABLE 4\|Experiment n°Total CO2 captured (mol)Slurry volume (mL)Slurry conc. (g/L)Total solids. (g)CO2 captured, as % of theoretical maximumSlurry additivesTemp. (°C)Duration (h)Solid products detected10.06412605013.035Na2CO3: 21.15 g/L3524Hydromagne site20.07242605013.040Na2CO3: 53.85 g/L3524Hydromagne site30.13632605013.075NaHCO3: 53.85 g/L3530Hydromagne site40.035226011.52.99843526Artinite\|[0088] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite and, in one case, artinite, which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 6\|[0089] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometre sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950°C), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio (molar ratio approximately 1:1.3). About 5kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950°C for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by XRF spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3 and 33.4% sodium expressed as Na2O. An XRD analysis showed the major phases present in the product to be Na2MgSiO4 and periclase (MgO).\|EXAMPLE 7\|[0090] The reaction products of Example 2 (referred to hereinafter as "product X") and of Example 6 (referred to hereinafter as "product XS") were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75g of the solid were added to 1.5 litres of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal litres per hour at close to one atmosphere absolute pressure. The reactor contents were maintained at 70°C by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements by ICP. The solid filter-cakes were dried at 110°C and then analysed by XRF spectrometry for elemental composition, by XRD for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0091] The results for three different product samples are given in the following Table\|TABLE 5\|Experiment N° ; anhydrous product usedDuration (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %5 Product X3.5420Hydromagnesite31.215.918.20.65961 Product X4.0600Hydromagnesite30.316.418.80.5637 Product XS4.0205Hydromagnesite27.717.219.70.471(1) In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0092] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields of the order of 60-70% of the total magnesium in the starting material in about 3.5 to 4 hours. Based on XRF analyses of the solid phases coupled with ICP analyses of the liquid phase, it is estimated that roughly 90% of the initial Na and 50% of the initial Cr in the product leached out during the experiment.\|EXAMPLE 8\|Formation of eitelite.\|[0093] The procedure of Example 7 was repeated using two slurries (prepared from products X and XS from Examples 2 and 6, respectively) at a concentration of 150g/L, i.e. three times the concentration used in Example 7.\|[0094] During the 3 first hours the same trends were observed as those in Example 7. But after 4 hours, XRD revealed the presence of eitelite as well as hydromagnesite. The results are given in the following Table.\|TABLE 6\|Experiment N° ; anhydrous product usedDuratio n (h)Blaine specific surface area of anhydrous product, m2/kgMain crystalline phases detected in dried filter-cakeTotal Mg content of dried filter-cake, expressed as MgO, %CO2 content of dried filter-cake, %Estimated Mg in hydromagnesite expressed as %MgO in filter-cakeMg in aqueous phase expressed as %MgO relative to filter-cakeEstimated degree of reaction of MgO in anhydrous product, %8 Product X4.0600Hydromagnesite & eitelite28.0616.4518.830.567.129 Product XS4.0600Hydromagnesite & eitelite25.7415.8218.110.870.37\|EXAMPLE 9\|Effectiveness of water leaching\|[0095] 50g of product X was washed in 1 L deionised water 6 times in series (15minutes stirring in between at room temperature and atmospheric pressure, i.e. 25°C and 1 bar). Each time a small sample was taken to analyse the solids and the liquids. The XRF results for product X coupled with ICP solution analyses lead to the results given in the following Table, which the percentages of each element leached from the product are given as a function of the number of washing steps.\|TABLE 7\|% leachedSiCaMgKNaSCrWashing 19.850.460.0019.7636.4413.7746.12Washing 23.200.090.001.948.690.601.30Washing 31.410.020.000.253.470.040.21Washing 41.220.020.000.033.530.130.32Washing 50.750.020.000.021.870.140.12Washing 60.510.050.000.001.300.050.08TOTAL16.940.660.0122.0055.3114.7348.15\|[0096] The first washing step was clearly the most efficient. Therefore 500g of product X were washed in the same conditions, the solid was then filtered and dried overnight at 110°C. Finally the same carbonation experiment as described in Example 8 was performed on this solid product. This time XRD analysis revealed only hydromagnesite; no eitelite was detected. This shows that washing can be used to enhance Na recycling in the process.\|[0097] The analysis of the solution obtained after the first washing (table below) showed it to have a high pH and to contain about 4000mg/L of Na and 637 mg/L of Si, the other elements being present in much smaller amounts. On this basis, the solution was estimated to contain about 23 milimoles/litre of sodium metasilicate (Na2SiO3 and 130 millimoles/litre of sodium hydroxide (NaOH), possibly also including some carbonate ions.\|TABLE 8\|In mg/l (elements)SiCaMgKNaSCrWashing 1637.50.2990.2674.140001.38\|EXAMPLE 10\|Hydromagnesite formation at 60°C\|[0098] 1 L of a 50g/L slurry of product X was prepared and poured into a 2L autoclave. The system was closed and 1 L of pure CO2 at 10 bars was added without purging the residual air, after which the slurry was stirred and heated up to 60°C (which roughly corresponds to the dew point of exhaust gases in a cement plant). After 2 hours the pressure dropped to close to atmospheric and heating of the autoclave was stopped. The next day, the slurry was filtered and dried overnight at 110°C. XRD revealed hydromagnesite as the main crystalline product.\|EXAMPLE 11\|Formation of magnesite as main product at 120°C.\|[0099] The procedure of Example 10 was repeated but at 120°C (a typical temperature for exhaust gases from a cement plant) using the same autoclave, and adding CO2 each time the pressure dropped close to two bars (the equilibrium water vapour pressure at 120°C). Three additions of CO2 up to 10 bars were made in the space of one day. XRD on the dried solid revealed magnesite (MgCO3 to be the main product, but also showed some traces of magnetite (Fe3O4). ICP analysis of the aqueous phase showed 90% leaching of Na. The combined CO2 content in the solids was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser and showed that the amount of MgCO3 present accounted for about 47% of the original Mg in Product X.\|EXAMPLE 12\|Selective separation of chromium by reduction in solution.\|[0100] Powdered product X was stirred with deionised water for 15 minutes at a 2:1 water:solids mass ratio. The yellow-coloured aqueous phase was filtered and a sample taken for ICP analysis. Excess ferrous sulfate (FeSO4), a reducing agent, was then added in powder form to the solution, after which a chromium-containing precipitate formed. The liquid was again filtered, giving a colourless solution which was again analysed by ICP. The chromium content of the yellow-coloured aqueous phase was 772 mg/L. The colourless solution contained only 29 mg/L of chromium.\|[0101] These results, when compared with the analysis of the raw materials, indicated that about 50% of the total chromium in the original raw material (olivine) was converted into a readily soluble (chromate) form by the process used to make "product X," and 96% of the Cr leached into the solution was precipitated by addition of ferrous sulfate.\|EXAMPLE 13\|Concentration of hydromagnesite from the solid residues by flotation\|[0102] Separation tests were performed by flotation on the carbonated products produced from the application of the process to olivine and serpentine, similarl to the products shown, respectively, for experiments 5 and 7 in the table of Example 7. Combinations of sodium oleate, carboxymethylcellulose (CMC) and methyl isobutyl carbinol (MIBC) were used in the aqueous phase sequentially to disperse the solids in the form of a slurry at a solids concentration of 90g/L.\|[0103] First sodium oleate was added to the slurry and stirred for 5 minutes in a beaker in order to render carbonated particles hydrophobic. Then CMC was added to depress silicate hydrophobicity, followed by a further 5 minutes of stirring; and finally MIBC was added in order to stabilise the foam formed by air bubbling.\|[0104] Air was bubbled through the treated slurry in a miniature flotation cell, and the solids carried over by the foam were collected as "concentrate." The residual solids were collected as "tailings." Results of four such experiments are presented in the table below. The CO2 content was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser. The CO2 contents of the concentrates were typically 3-4 times greater than those of the tailings, showing that hydromagnesite can be effectively separated by flotation in this manner.\|[0105] The XRD results confirm the separation. They are expressed in a qualitative way by different symbols expressing the probability of a phase presence:\| (o) not present,\| () possibly present,\| (X) definitely present,\| (X+) present in abundance.\|TABLE 9\|Chemical additive (dosage, ppm)Test 1Test 2Test 3Test 4Sodium oleate1500100020001000CMC200200200200MIBC20202020Product tested by flotation:Carbonated "product X"Carbonate "product X"Carbonated "product X"Carbonated "product XS"Results of flotati on testsTailingsCon centrateTailingsConcentrateTailingsConcentrateTailingsConcentrateComponents measured by chemical analysisSiO2 %34.117.633.718.533.822.033.316.9Fe2O3 %6.43.46.43.66.44.36.93.0MgO %34.637.234.537.233.936.929.235.9Na2O %2.31.32.31.42.61.32.31.2LOI %22.340.022.638.922.735.126.241.6CO2 %5.722.25.820.25.717.39.423.0Phases detected by XRDSodium magnesium silicate00000000PericlaseXXX*OlivineXXX00HydromagnesiteXX+XX+XX+XX+\|EXAMPLE 14\|[0106] (not according to the invention) Ground natural talc from Luzenac (France) with nominal composition Mg3Si4O10(OH)2 and containing some minor impurities (1.1% Al2O3, 0.9 % Fe2O3 and 0.9% CaO by mass) was mixed with anhydrous sodium carbonate (Na2CO3) at a 4863:5136 mass ratio (molar ratio approximately 1:1). The composition was chosen in order to obtain an atomic ratio of 2:1 Na:Si in the final sample. 20.5g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. The sample was heated at 900°C for 1 hour, followed by cooling in air. It was weighed before and after treatment and the measured loss on ignition of 23.3% was consistent with evaporation of carbon dioxide from the sodium carbonate plus bound water from the talc; it represents about 95% of the theoretical value for complete reaction of 24.6%. The phase constitution of the reacted sample was determined by X-ray diffraction: the main products detected were Na2MgSiO4 and Na2SiO3.	Family Number\|(66070146)\|66070146\|Advantages / Prev. Drawbacks\|(EP2735553 B1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|(EP2735553 A1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|	Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-2251/402\|B01D-2253/106\|B01D-2257/504\|C01B-033/20\|C01F-005/06\|C01F-005/14\|C01F-005/24\|C04B-002/10/2\|C04B-009/00\|C04B-028/10\|C04B-028/18/4\|C04B-2111/00019\|Y02C-020/40\|Y02P-020/151\|Y02P-040/18\|Y02P-040/40	(GR1) C04B-028/18/4[RK1]; C04B-040/02/31[RK2]	B01D-053/62\|B01D-2251/402\|B01D-2253/106\|B01D-2257/504\|C01B-033/20\|C01F-005/06\|C01F-005/14\|C01F-005/24\|C04B-002/10/2\|C04B-009/00\|C04B-028/10\|C04B-028/18/4\|C04B-2111/00019\|Y02C-020/40\|Y02P-020/151\|Y02P-040/18\|Y02P-040/40	B01D-053/62\|C01B-033/20\|C01D-007/00\|C01F-005/06\|C01F-005/14\|C01F-005/24\|C04B-002/10	B01D-053/62\|C01B-033/20\|C01D-007/00\|C01F-005/06\|C01F-005/14\|C01F-005/24\|C04B-002/10\|C04B-009/00			CN119370855	CN119370855 113183772 WHO=Examiner SELF=N CAT=A	US20120291675\|WO200769902\|US6054106\|WO2009156740\|EP2508496\|US5085838\|EP2532624\|WO201097451\|CA1189288\|US20120291675\|WO2009156740\|US20040213705\|US20040213705\|US5085838	US20120291675 6949869 WHO=Examiner SELF=N CAT=Y\|WO200769902 6679764 WHO=Examiner SELF=N CAT=Y\|US6054106 490034 WHO=Examiner SELF=N CAT=X CAT=Y\|WO2009156740 1844239 WHO=Examiner SELF=N CAT=X CAT=D\|EP2508496 15070805 WHO=Examiner SELF=N CAT=X\|US5085838 42717873 WHO=Examiner SELF=N CAT=X\|EP2532624 15065813 WHO=Examiner SELF=N CAT=E\|WO201097451 44611783 WHO=Examiner SELF=N CAT=A\|CA1189288 3817049 WHO=Examiner SELF=N CAT=A\|US20120291675 6949869 WHO=Applicant SELF=N\|WO2009156740 1844239 WHO=Applicant SELF=N\|US20040213705 1759232 WHO=Examiner SELF=N\|US20040213705 1759232 WHO=Applicant SELF=N\|US5085838 42717873 WHO=Applicant SELF=N		EP2532624; US5085838; EP2508496; US20120291675; WO200769902; CA1189288; WO201097451; US6054106; US20040213705; XP002994928; WO2009156740; US5085838; US20120291675; US20040213705; WO20070159902; WO2009156740	(EP2735553)\|Examiner references\|-O'CONNOR W K ET AL: "Carbon dioxide sequestration by direct mineral carbonation: process mineralogy of feed and products", MINERALS AND METALLURGICAL PROCESSING,, vol. 19, no. 2, 1 May 2002 (2002-05-01), pages 95 - 101, XP002994928, ISSN: 0747-9182\|	LAPSED	(EP2735553)\|LAPSED	DEAD	(EP2735553)\|DEAD	(EP2735553)\|LEGAL DETAILS FOR EP2735553\|Actual or expected expiration date=2020-10-30\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2012-11-27\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP12306468\|Application date=2012-11-27\|Standardized application number=2012EP-0306468\|Event publication date=2014-05-27\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2014-05-28\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication 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event=2019-11-27\|Corresponding cc:\|Designated or member state=GB\|Event publication date=2020-10-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=GB\|MEMBER STATE LEGAL DETAILS FOR GR\|Actual or expected expiration date=2017-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=GR\|Event publication date=2017-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=GR\|MEMBER STATE LEGAL 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notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=IE\|MEMBER STATE LEGAL DETAILS FOR IS\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IS\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IS\|MEMBER STATE LEGAL DETAILS FOR IT\|Actual or expected expiration date=2018-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=IT\|Event publication date=2018-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=IT\|MEMBER STATE LEGAL DETAILS FOR LI\|Actual or expected expiration date=2020-07-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LI\|Event publication date=2020-07-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LI\|MEMBER STATE LEGAL DETAILS FOR LT\|Actual or expected expiration date=2017-08-25\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2017-08-25\|Event code=EP/REG\|Event code=LT/MG4D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Invalidated european patent\|Europos patentai, laikomi ab initio negaliojanciais\|Corresponding cc:\|Designated or member state=LT\|Event publication date=2017-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LT\|MEMBER STATE LEGAL DETAILS FOR LU\|Actual or expected expiration date=2018-08-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LU\|Event publication date=2018-08-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=LU\|MEMBER STATE LEGAL DETAILS FOR LV\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=LV\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=LV\|MEMBER STATE LEGAL DETAILS FOR MC\|Actual or expected expiration date=2018-06-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MC\|Event publication date=2018-06-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MC\|MEMBER STATE LEGAL DETAILS FOR MK\|Actual or expected expiration date=2019-11-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MK\|Event publication date=2019-11-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=MK\|MEMBER STATE LEGAL DETAILS FOR MT\|Actual or expected expiration date=2018-09-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=MT\|Event publication date=2018-09-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES\|Corresponding cc:\|Designated or member state=MT\|MEMBER STATE LEGAL DETAILS FOR NL\|Actual or expected expiration date=2017-04-05\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2017-08-09\|Event code=EP/REG\|Event code=NL/MP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Reference to a national code\|Patent voided (invalid in the netherlands as no translation has been filed)\|Effective date of the event=2017-04-05\|Corresponding cc:\|Designated or member state=NL\|Event publication date=2017-09-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NL\|MEMBER STATE LEGAL DETAILS FOR NO\|Actual or expected expiration date=2017-10-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=NO\|Event publication date=2017-10-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=NO\|MEMBER STATE LEGAL DETAILS FOR PL\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PL\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PL\|MEMBER STATE LEGAL DETAILS FOR PT\|Actual or expected expiration date=2020-05-29\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=PT\|Event publication date=2020-05-29\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=PT\|MEMBER STATE LEGAL DETAILS FOR RO\|Actual or expected expiration date=2018-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RO\|Event publication date=2018-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RO\|MEMBER STATE LEGAL DETAILS FOR RS\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RS\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=RS\|MEMBER STATE LEGAL DETAILS FOR SE\|Actual or expected expiration date=2017-11-30\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SE\|Event publication date=2017-11-30\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SE\|MEMBER STATE LEGAL DETAILS FOR SI\|Actual or expected expiration date=2018-05-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SI\|Event publication date=2018-05-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SI\|MEMBER STATE LEGAL DETAILS FOR SK\|Actual or expected expiration date=2018-01-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SK\|Event publication date=2018-01-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SK\|MEMBER STATE LEGAL DETAILS FOR SM\|Actual or expected expiration date=2018-02-28\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=SM\|Event publication date=2018-02-28\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=SM\|MEMBER STATE LEGAL DETAILS FOR TR\|Actual or expected expiration date=2020-03-31\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=TR\|Event publication date=2020-03-31\|Event code=EP/PG25\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Lapsed in a contracting state announced via postgrant inform. from nat. office to EPO\|LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT\|Corresponding cc:\|Designated or member state=TR	(EP2735553)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR		https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=9ru+nrv5jojEpfCxziNKemkyFX8ClgOuNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=EP2735553&ekey=947&xpn=EP2735553&kind=B1	https://register.epo.org/application?number=EP12306468	https://permalink.orbit.com/RenderStaticFirstPage?XPN=ckl9VSHqF2eeccOAsqvWAnfDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	EP	(EP2735553)\|FR\|(EP2735553)\|FR	(EP2735553)\|NAME=LAFARGE 61, rue des Belles Feuilles , CITY=75116 Paris , COUNTRY=FR , REG=100163084\|(EP2735553)\|NAME=LAFARGE 61, rue des Belles Feuilles , CITY=75116 Paris , COUNTRY=FR , REG=100163084	(EP2735553)\|AT\|(EP2735553)\|FR	(EP2735553)\|NAME=Keschmann, Marc;Haffner und Keschmann Patentanwälte GmbH Schottengasse 3a , CITY=1014 Wien , COUNTRY=AT , REG=101393339\|(EP2735553)\|NAME=Mérigeault, Shona;Lafarge Département Propriété Industrielle (DPI) 95 Rue du Montmurier BP 9 , CITY=38291 Saint Quentin Fallavier Cedex , COUNTRY=FR , REG=101004378	(EP2735553)\|FR; FR; FR\|(EP2735553)\|FR; FR; FR	(EP2735553)\|NAME=Gartner, Ellis Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=Pisch, Alexander Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=Meyer, Vincent Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR\|(EP2735553)\|NAME=Gartner, Ellis Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=Pisch, Alexander Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=Meyer, Vincent Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=38291 Saint Quentin Fallavier, COUNTRY=FR	(EP2735553)\|2	1	1					(EP2735553)\|Number of Claims: NCL=6\|Primary examiner: Theodoridou, K\|\|(EP2735553)\|Number of Claims: NCL=10\|Primary examiner: Theodoridou, K\|		(EP2735553)\|ENGLISH (ENG)	(EP2735553)\|Patent\|(EP2735553)\|Patent	Titre: (EP2735553)\|Process for the treatment of a silicate mineral Résumé: (EP2735553)\|The invention provides a process for the preparation of a first product comprising an alkali metal magnesium orthosilicate and (i) magnesium oxide or (ii) an alkali metal silicate, which process comprises the reaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R 2 O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO 2 , being from 4:1 to 1:4, and contacting the first product with water to produce a second product comprising magnesium hydroxide and isolating or producing further useful products from the second product.	42	Abstract	gpt-4o-mini	uncertain	The process involves silicate minerals and alkali metal carbonates, but it is not explicitly focused on CO₂ capture or enhanced weathering for carbon sequestration.
46	EP12306468\|EP12306469\|EP13795508\|WOEP2013/074732	WOEP2013/074732\|RU2015125492\|AU2013351282\|CN201380061823\|US14/647,277\|JP2015543468\|EP13795508\|MX2015006607\|KR10-2015-7016739\|CA2892325	RU2654983\|AU2013351282\|CN104812468\|US9631257\|RU2015125492\|JP2015536897\|US20150299823\|EP2925426\|MX2015006607\|KR10-2015-0088845\|CN104812468\|AU2013351282\|CA2892325\|WO2014/082996	66131709	WO2014/082996 A1 2014-06-05 [WO201482996]\|RU2654983 C2 2018-05-23 [RU2654983]\|RU2015125492 A 2017-01-11 [RU2015125492]\|AU2013351282 B2 2018-03-01 [AU2013351282]\|AU2013351282 A1 2015-06-18 [AU2013351282]\|CN104812468 B 2017-08-25 [CN104812468B]\|CN104812468 A 2015-07-29 [CN104812468]\|US9631257 B2 2017-04-25 [US9631257]\|US20150299823 A1 2015-10-22 [US20150299823]\|JP2015536897 A 2015-12-24 [JP2015536897]\|EP2925426 A1 2015-10-07 [EP2925426]\|MX2015006607 A 2015-08-05 [MX2015006607]\|KR10-2015-0088845 A 2015-08-03 [KR20150088845]\|CA2892325 A1 2014-06-05 [CA2892325]	2012-11-27\|2013-11-26	2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26\|2013-11-26	2018-05-23\|2018-03-01\|2017-08-25\|2017-04-25\|2017-01-11\|2015-12-24\|2015-10-22\|2015-10-07\|2015-08-05\|2015-08-03\|2015-07-29\|2015-06-18\|2014-06-05\|2014-06-05	\|(US9631257)\|2017-04-25\|\|\|(CN104812468B)\|2017-08-25\|(RU2654983)\|2018-05-23\|(AU2013351282)\|2018-03-01\|\|\|	(EP2925426)\|2018-04-10\|(US9631257)\|2021-05-31\|(WO2014/082996)\|2016-05-27\|(JP2015536897)\|2018-08-22\|(CN104812468)\|2019-11-26\|(RU2654983)\|2019-11-27\|(AU2013351282)\|2020-06-25\|(MX2015006607)\|2033-11-26\|(KR10-2015-0088845)\|2018-12-27\|(CA2892325)\|2020-08-31	(EP2925426)\|Process for the treatment of a silicate mineral	(EP2925426)\|The invention provides a process for the preparation of a second composition, said process comprising the steps of: -preparing a first compositioncomprising an alkali metal magnesium orthosilicate andoptionally either(i) magnesium oxide or(ii) an alkali metal silicate, byreaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R 2 O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO 2, being from 4:1 to 1:4, and -contacting the first composition with water to produce thesecond composition comprising an amorphous magnesium silicate hydrate (M-S-H). It is possible to isolateor producefurther useful products from the second composition.	HOLCIM TECHNOLOGY\|LAFARGE	(EP2925426)\|Lafarge SA ([FR])\|(US9631257)\|LAFARGE ([FR])\|(US20150299823)\|LAFARGE ([FR])\|(WO2014/082996)\|LAFARGE ([FR])\|(JP2015536897)\|LAFARGE SA\|(CN104812468)\|LAFARGE SA ([FR])\|(CN104812468)\|LAFARGE SA ([FR])\|(RU2654983)\|LAFARGE ([FR])\|(RU2015125492)\|LAFARGE ([FR])\|(AU2013351282)\|Lafarge\|(AU2013351282)\|Lafarge\|(MX2015006607)\|LAFARGE ([FR])\|(KR10-2015-0088845)\|LAFARGE\|(CA2892325)\|LAFARGE ([FR])	PISCH ALEXANDER\|GARTNER ELLIS\|MEYER VINCENT	(EP2925426)\|PISCH, Alexander\|GARTNER, Ellis\|MEYER, Vincent	(EP2925426)\|Soares, Luis Filipe;Lafarge ([FR])\|Reg. Nb: 101513670\|(US9631257)\|Pillsbury Winthrop Shaw Pittman LLP\|(WO2014/082996)\|MERIGEAULT, Shona ([FR])\|(JP2015536897)\|MURAKOSHI, Satoshi\|Reg. Nb: 100126572\|OBATA Yuichi\|Reg. Nb: 100125195\|(CN104812468)\|CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM\|Reg. Nb: 11314\|(RU2654983)\|LLC LAW FIRM GORODISSKY AND PARTNERS\|(AU2013351282)\|Watermark Intellectual Property Pty Ltd ([AU])\|(MX2015006607)\|CARLOS PÉREZ DE LA SIERRA\|(KR10-2015-0088845)\|KOREANA PATENT FIRM\|Reg. Nb: 920011000013\|(CA2892325)\|NORTON ROSE FULBRIGHT CANADA LLP/S.E.N.C.R.L., S.R.L. ([CA])	(US9631257)\|However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible.\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled.\|Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300° C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eitelite, Na2CO3.MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|	(US9631257)\|1. A process for the treatment of a silicate mineral, said process comprising: preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 600° C. to 1000° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, wherein the reaction is obtained by contacting the alkali metal carbonate compound and the magnesium silicate to each other in a solid state, and contacting the first composition with water to produce a second composition comprising an amorphous magnesium silicate hydrate (M-S-H).\|	(US9631257)\|It was found to contain nesquehonite (MgCO3.3H2O), nahcolite (NaHCO3), trona (Na3H(CO3)2.2H2O), and sodium carbonate mono-hydrate (Na2CO3.H2O).\|The present invention accordingly provides a process for the preparation of a second composition, said process comprising the steps of: - preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 500 to 1200° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, and - contacting the first composition with water to produce the second composition comprising an amorphous magnesium silicate hydrate (M-S-H).\|This invention relates to a process for the treatment of a silicate mineral.\|	(EP2925426)\|SILICATE MINERAL(100,1)\|SILICATE MINERAL TREATMENT(100,1)\|\|(US9631257)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,4)\|SILICATE MINERAL TREATMENT(100,4)\|MAGNESIUM SILICATE(94,63)\|AMORPHOUS SILICA PRECIPITATE(80,2)\|SILICA PRECIPITATE(70,1)\|ALKALI METAL CARBONATE(68,49)\|MAGNESIUM ORTHOSILICATE(66,14)\|OUTGOING HOT GAS(64,1)\|MOLAR RATIO(62,11)\|MOVING GRATE FURNACE(62,2)\|OUTGOING HOT SOLID(58,1)\|NA2CO(57,2)\|ALKALI METAL SILICATE(56,12)\|ALKALI METAL(54,76)\|MAGNESIUM SILICATE HYDRATE(54,6)\|SUBSTEP(54,2)\|ALKALI METAL BICARBONATE(52,5)\|NEUTRALIZING(50,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(48,12)\|INCOMING SOLID(48,1)\|NAHCOLITE(48,1)\|MAGNESIUM OXIDE(44,16)\|FURNACE(42,8)\|MOVING GRATE(38,5)\|INCOMING COMBUSTION AIR(38,1)\|NET ENERGY CONSUMPTION(37,2)\|USEFUL PRODUCT(37,2)\|METHANEDIONE(36,5)\|COUNTERCURRENT HEAT EXCHANGE(36,3)\|TEMPERATURE ELEVATION(36,1)\|CARBONATED SHAPED ARTICLE(35,3)\|NESQUEHONITE(34,7)\|PELLET(33,24)\|MGCO(33,14)\|EITELITE(31,5)\|CO2(29,29)\|AMBIENT TEMPERATURE(28,2)\|MAGNESIUM OXIDE MOLAR RATIO(28,1)\|X H2O(26,1)\|UNREACTED OLIVINE(24,3)\|COMPLEX ALKALI METAL(24,1)\|SODIUM CARBONATE MONO HYDRATE(24,1)\|BED(23,5)\|HEAT EXCHANGE(22,4)\|PREHEATER CYCLONE TOWER(22,1)\|OLIVINE SAND(21,3)\|PLATINUM CRUCIBLE(21,3)\|SOLID PRODUCT(20,10)\|LAB FURNACE(20,4)\|XRF SPECTROMETRY(20,2)\|R2MGSIO(18,9)\|GASEOUS CO2(18,4)\|SODIUM BICARBONATE(18,2)\|ASBESTOS FIBRILLAR(18,1)\|DECARBONATED NODULE(18,1)\|MAGNESIUM XRD SILICATE(18,1)\|OBSCURATION STABILIZATION(18,1)\|EARTH CRUST(17,2)\|LASER GRANULOMETRY(17,2)\|RESIDUAL R2CO(17,2)\|MG2SIO(16,7)\|FINE SUSPENSION(16,4)\|CHROMIUM COMPOUND(16,3)\|COUNTER CURRENT HEAT EXCHANGE(16,1)\|DECARBONATED PELLET(16,1)\|FORSTERITE OLIVINE(16,1)\|METHANEDIONE GAS LIBERATION(16,1)\|NA2MGSIO(14,6)\|TAILING(14,6)\|ENERGY EFFICIENCY(14,3)\|SAMPLE REACTION(14,3)\|ANHYDROUS MAGNESIUM SILICATE(14,2)\|SLURRY ADDITIVE(14,2)\|ABSORB METHANEDIONE(14,1)\|CO2 NET CONSUMER(14,1)\|CO2 SLURRY(14,1)\|DISSOLUTION BEHAVIOR(14,1)\|HEAT TRANSFER(14,1)\|HELICOIDAL TEFLON(14,1)\|MAGNETITE TRACE(14,1)\|METHANEDIONE EVAPORATION(14,1)\|MINIATURE FLOTATION CELL(14,1)\|PHOTOMETRY HYDROMAGNESITE MG(14,1)\|PREHEATER TOWER(14,1)\|SILICATE HYDROPHOBICITY(14,1)\|MAGNESIUM SILICATE WATER(13,11)\|ALKALI METAL OXIDE(13,7)\|AUTOCLAVE(13,5)\|PERICLASE(13,5)\|HUMIDITY CONDITION(13,4)\|PARTICULATE(12,4)\|POWDERED PRODUCT(12,4)\|PRODUCT RICH(12,4)\|BURNING ZONE(12,2)\|BLAINE MG(12,1)\|CARBONATE PARTICLE(12,1)\|CO2 UPTAKE(12,1)\|COMPANION PELLET(12,1)\|CONCENTRATE CO2 CONTENT(12,1)\|EFFLORESCENCE SAMPLE(12,1)\|ENHANCE NA RECYCLING(12,1)\|GROUND OLIVINE MIX(12,1)\|LASER GRANULOMETER(12,1)\|NODULE RISK(12,1)\|PERFECTLY BALANCED EQUATION(12,1)\|PRODUCT HECTORITE MANUFACTURER(12,1)\|SAMPLE DEAGGLOMERATION(12,1)\|SLURRY TEMP(12,1)\|SUSPENSION PREHEATER(12,1)\|UNREACTED ANHYDROUS COMPOUND(12,1)\|UNTREATED PELLET(12,1)\|UNTREATED RESIDUE(12,1)\|ANHYDROUS DURATION PRODUCT(11,2)\|COLORLESS SOLUTION(11,2)\|GAS ANALYZER(11,2)\|MGO EXPRESSION(11,2)\|REACTED SAMPLE PHASE CONSTITUTION(11,2)\|SI CA MG(11,2)\|SODIUM MAGNESIUM ORTHOSILICATE(11,2)\|REACTION PRODUCT(10,8)\|ALKALINE SOLUTION(10,3)\|COMBUSTION EXHAUST GAS(10,3)\|HYDROCYCLONE(10,3)\|QUENCHING(10,3)\|ANALYSIS NA2O(10,1)\|ARTINITE MG(10,1)\|CO2 10H2O(10,1)\|CO2 EMISSION(10,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(10,1)\|CURING REGIME(10,1)\|DECARBONATION REACTION(10,1)\|EARTH MANTLE COMPONENT(10,1)\|EXPERIMENT CAPTURED VOLUME(10,1)\|FERMENTATION RESIDUE GAS(10,1)\|FINE NESS(10,1)\|FINE SAND GRANULOMETRY(10,1)\|FLOTATION AID(10,1)\|INORGANIC IMPURITY(10,1)\|LAYERED DOUBLE HYDROXIDE(10,1)\|MINERAL CARBONATE(10,1)\|MOVING GRATE COOLER(10,1)\|OLIVINE SAMPLE(10,1)\|PRECIPITATED SILICA(10,1)\|R2O MOLAR RATIO(10,1)\|RAW MAGNESIUM SILICATE(10,1)\|SILICATE ANION(10,1)\|SUSPENSION AGITATION(10,1)\|SYNTHETIC HECTORITE(10,1)\|UNREACTED MAGNESIUM SILICATE(10,1)\|UNREACTED PARTICLE(10,1)\|VESSEL PRESSURIZATION(10,1)\|WET CARBONATED PELLET(10,1)\|WORKING SESSION(10,1)\|R2SIO(9,5)\|SODIUM OLEATE(9,5)\|CARBOXYMETHYLCELLULOSE(9,3)\|CEMENT PLANT(8,4)\|HOT GAS(8,4)\|HYDROXY CARBONATE WATER(8,4)\|ROTARY KILN(8,4)\|ACTINOLITE(8,2)\|AMOSITE(8,2)\|AMPHIBOLE(8,2)\|ANHYDROUS SODIUM CARBONATE(8,2)\|ANTHOPHYLLITE(8,2)\|BRUCITE(8,2)\|CENTRIFUGATION(8,2)\|CHRYSOTILE(8,2)\|COMPLEX MAGNESIUM(8,2)\|ENSTATITE(8,2)\|LIQUID FILTRATE(8,2)\|MEASURED LOI DATA(8,2)\|MGO SILICA MOLAR RATIO(8,2)\|MIXED POWDER(8,2)\|MOLDING(8,2)\|PYROXENE(8,2)\|SIEVING(8,2)\|SODIUM CARBONATE POWDER(8,2)\|SYMBOL(8,2)\|TREMOLITE(8,2)\|ULTRASOUND(8,2)\|ALKALI BICARBONATE SOLUTION(8,1)\|ALKALI SOLUBLE IMPURITY(8,1)\|BASIC MAGNESIUM ORTHOSILICATE(8,1)\|BIOMASS DERIVED FUEL(8,1)\|BLUE DIODE(8,1)\|CALCULATION MATRIX(8,1)\|CARBONATABLE SOLID(8,1)\|CARBONATE ION(8,1)\|CARBONATED PRODUCT(8,1)\|CHROMIUM CONTENT(8,1)\|CO2 ATMOSPHERE(8,1)\|CO2 GRAM(8,1)\|COARSE UNREACTED SOLID(8,1)\|COMBINED CO2 QUANTITATIVE DETECTION(8,1)\|COMPRESSIVE LOAD(8,1)\|COOLED PELLET(8,1)\|CRUSHED SAMPLE(8,1)\|CRYSTALLINE COMPOUND(8,1)\|CURING CHAMBER(8,1)\|CYLINDRICAL MOLD(8,1)\|CYLINDRICAL PELLET(8,1)\|DISSOLVED ANION(8,1)\|ESTIMATED MG(8,1)\|GROUND NATURAL TALC(8,1)\|HOT NODULE HEAT(8,1)\|HOT QUENCHED SOLID(8,1)\|INCOMING COMBUSTION AIR PREHEATER(8,1)\|IRON ISOLATION(8,1)\|MAGNESIA FINE PARTICLE(8,1)\|MAGNESIUM SILICATE MINERAL(8,1)\|MAXIMUM CO2 CAPTURE(8,1)\|NATURALLY OCCURRING MINERAL(8,1)\|OUTGOING SOLID PARTICLE(8,1)\|PHASE PROBABILITY(8,1)\|PLUS MAGNESIUM(8,1)\|POROUS BED(8,1)\|POWDER SELF NODULIZE(8,1)\|PREHEATER TOP CYCLONE(8,1)\|PRESSED PELLET(8,1)\|QUALITATIVE PHASE(8,1)\|QUICK WASH(8,1)\|REACTION ESCAPE(8,1)\|REACTOR CONTENT(8,1)\|RED HE NE LASER(8,1)\|RUBBER BOWL(8,1)\|SESQUIHYDRATE(8,1)\|SILICA MOLE(8,1)\|SODIUM SILICATE MILIMOLE LITER(8,1)\|SOLUBLE SALT(8,1)\|SORT REACTION(8,1)\|STEEL CRUCIBLE(8,1)\|SULFUR CONTENT(8,1)\|TREATED SLURRY(8,1)\|WEAK PEAK(8,1)\|XRD DATA RIETVELD ANALYSIS(8,1)\|DEIONIZED WATER(7,5)\|METHYL ISOBUTYL CARBINOL(7,5)\|ALKALI METAL CATION(7,3)\|ATMOSPHERE PRESSURE(7,3)\|DRY CONDITION(7,3)\|FE3O(7,3)\|USEFUL PRODUCT STREAM(7,3)\|NAFEO(7,2)\|SIEVE(7,2)\|4MGO FE2O(6,1)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|AIR BUBBLING(6,1)\|ALKALINE AQUEOUS SOLUTION(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANHYDROUS PRODUCT(6,1)\|ANTIGORITE(6,1)\|AQUEOUS ACID(6,1)\|AQUEOUS PHASE ICP ANALYSIS(6,1)\|AQUEOUS SOLUTION CHEMICAL SPECIES(6,1)\|ATMOSPHERIC PRESSURE CARBONATION(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|CALCINATION(6,1)\|CAO SILICA MOLAR RATIO(6,1)\|CARBONATE PRODUCT(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|CO2 MG(6,1)\|COMPRESSION MACHINE(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|CRYSTALLINE PRODUCT(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|EXCESS FERROUS SULFATE(6,1)\|FAYALITE(6,1)\|FE2SIO(6,1)\|FEO SILICA MOLAR RATIO(6,1)\|FILTER CAKE DRYING(6,1)\|\|(US20150299823)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,4)\|SILICATE MINERAL TREATMENT(100,4)\|MAGNESIUM SILICATE(89,62)\|AMORPHOUS SILICA PRECIPITATE(80,2)\|SILICA PRECIPITATE(70,1)\|MAGNESIUM ORTHOSILICATE(66,14)\|OUTGOING HOT GAS(64,1)\|ALKALI METAL CARBONATE(63,48)\|MOLAR RATIO(62,11)\|MOVING GRATE FURNACE(62,2)\|OUTGOING HOT SOLID(58,1)\|NA2CO(57,2)\|ALKALI METAL SILICATE(56,12)\|MAGNESIUM SILICATE HYDRATE(54,6)\|SUBSTEP(54,2)\|ALKALI METAL(52,75)\|ALKALI METAL BICARBONATE(52,5)\|CARBONATED SHAPED ARTICLE(52,4)\|NEUTRALIZING(50,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(48,12)\|INCOMING SOLID(48,1)\|NAHCOLITE(48,1)\|MAGNESIUM OXIDE(44,16)\|FURNACE(42,8)\|MOVING GRATE(38,5)\|INCOMING COMBUSTION AIR(38,1)\|NET ENERGY CONSUMPTION(37,2)\|USEFUL PRODUCT(37,2)\|METHANEDIONE(36,5)\|COUNTERCURRENT HEAT EXCHANGE(36,3)\|TEMPERATURE ELEVATION(36,1)\|NESQUEHONITE(34,7)\|PELLET(33,24)\|MGCO(33,14)\|EITELITE(31,5)\|CO2(29,29)\|AMBIENT TEMPERATURE(28,2)\|MAGNESIUM OXIDE MOLAR RATIO(28,1)\|MOLDING(24,3)\|UNREACTED OLIVINE(24,3)\|COMPLEX ALKALI METAL(24,1)\|SODIUM CARBONATE MONO HYDRATE(24,1)\|BED(23,5)\|HEAT EXCHANGE(22,4)\|PREHEATER CYCLONE TOWER(22,1)\|OLIVINE SAND(21,3)\|PLATINUM CRUCIBLE(21,3)\|SOLID PRODUCT(20,10)\|LAB FURNACE(20,4)\|XRF SPECTROMETRY(20,2)\|GASEOUS CO2(18,4)\|SODIUM BICARBONATE(18,2)\|ASBESTOS FIBRILLAR(18,1)\|DECARBONATED NODULE(18,1)\|MAGNESIUM XRD SILICATE(18,1)\|OBSCURATION STABILIZATION(18,1)\|EARTH CRUST(17,2)\|LASER GRANULOMETRY(17,2)\|RESIDUAL R2CO(17,2)\|R2MGSIO(16,7)\|FINE SUSPENSION(16,4)\|CHROMIUM COMPOUND(16,3)\|COUNTER CURRENT HEAT EXCHANGE(16,1)\|DECARBONATED PELLET(16,1)\|FORSTERITE OLIVINE(16,1)\|METHANEDIONE GAS LIBERATION(16,1)\|MG2SIO(14,6)\|NA2MGSIO(14,6)\|TAILING(14,6)\|ENERGY EFFICIENCY(14,3)\|SAMPLE REACTION(14,3)\|ANHYDROUS MAGNESIUM SILICATE(14,2)\|SLURRY ADDITIVE(14,2)\|ABSORB METHANEDIONE(14,1)\|CO2 NET CONSUMER(14,1)\|CO2 SLURRY(14,1)\|DISSOLUTION BEHAVIOR(14,1)\|HEAT TRANSFER(14,1)\|HELICOIDAL TEFLON(14,1)\|MAGNETITE TRACE(14,1)\|METHANEDIONE EVAPORATION(14,1)\|MINIATURE FLOTATION CELL(14,1)\|PHOTOMETRY HYDROMAGNESITE MG(14,1)\|PREHEATER TOWER(14,1)\|SILICATE HYDROPHOBICITY(14,1)\|MAGNESIUM SILICATE WATER(13,11)\|ALKALI METAL OXIDE(13,7)\|AUTOCLAVE(13,5)\|PERICLASE(13,5)\|HUMIDITY CONDITION(13,4)\|PARTICULATE(12,4)\|POWDERED PRODUCT(12,4)\|PRODUCT RICH(12,4)\|BURNING ZONE(12,2)\|BLAINE MG(12,1)\|CARBONATE PARTICLE(12,1)\|CO2 UPTAKE(12,1)\|COMPANION PELLET(12,1)\|CONCENTRATE CO2 CONTENT(12,1)\|EFFLORESCENCE SAMPLE(12,1)\|ENHANCE NA RECYCLING(12,1)\|GROUND OLIVINE MIX(12,1)\|LASER GRANULOMETER(12,1)\|NODULE RISK(12,1)\|PERFECTLY BALANCED EQUATION(12,1)\|PRODUCT HECTORITE MANUFACTURER(12,1)\|SAMPLE DEAGGLOMERATION(12,1)\|SLURRY TEMP(12,1)\|SUSPENSION PREHEATER(12,1)\|UNREACTED ANHYDROUS COMPOUND(12,1)\|UNTREATED PELLET(12,1)\|UNTREATED RESIDUE(12,1)\|ANHYDROUS DURATION PRODUCT(11,2)\|COLORLESS SOLUTION(11,2)\|GAS ANALYZER(11,2)\|MGO EXPRESSION(11,2)\|REACTED SAMPLE PHASE CONSTITUTION(11,2)\|SI CA MG(11,2)\|SODIUM MAGNESIUM ORTHOSILICATE(11,2)\|REACTION PRODUCT(10,8)\|ALKALINE SOLUTION(10,3)\|COMBUSTION EXHAUST GAS(10,3)\|HYDROCYCLONE(10,3)\|QUENCHING(10,3)\|ANALYSIS NA2O(10,1)\|ARTINITE MG(10,1)\|CO2 10H2O(10,1)\|CO2 EMISSION(10,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(10,1)\|CURING REGIME(10,1)\|DECARBONATION REACTION(10,1)\|EARTH MANTLE COMPONENT(10,1)\|EXPERIMENT CAPTURED VOLUME(10,1)\|FERMENTATION RESIDUE GAS(10,1)\|FINE NESS(10,1)\|FINE SAND GRANULOMETRY(10,1)\|FLOTATION AID(10,1)\|INORGANIC IMPURITY(10,1)\|LAYERED DOUBLE HYDROXIDE(10,1)\|MINERAL CARBONATE(10,1)\|MOVING GRATE COOLER(10,1)\|OLIVINE SAMPLE(10,1)\|PRECIPITATED SILICA(10,1)\|R2O MOLAR RATIO(10,1)\|RAW MAGNESIUM SILICATE(10,1)\|SILICATE ANION(10,1)\|SODIUM SILICATE MILIMOLE LITER(10,1)\|SUSPENSION AGITATION(10,1)\|SYNTHETIC HECTORITE(10,1)\|UNREACTED MAGNESIUM SILICATE(10,1)\|UNREACTED PARTICLE(10,1)\|VESSEL PRESSURIZATION(10,1)\|WET CARBONATED PELLET(10,1)\|WORKING SESSION(10,1)\|R2SIO(9,5)\|SODIUM OLEATE(9,5)\|CARBOXYMETHYLCELLULOSE(9,3)\|CEMENT PLANT(8,4)\|HOT GAS(8,4)\|HYDROXY CARBONATE WATER(8,4)\|ROTARY KILN(8,4)\|ACTINOLITE(8,2)\|AMOSITE(8,2)\|AMPHIBOLE(8,2)\|ANHYDROUS SODIUM CARBONATE(8,2)\|ANTHOPHYLLITE(8,2)\|BRUCITE(8,2)\|CENTRIFUGATION(8,2)\|CHRYSOTILE(8,2)\|COMPLEX MAGNESIUM(8,2)\|ENSTATITE(8,2)\|LIQUID FILTRATE(8,2)\|MEASURED LOI DATA(8,2)\|MGO SILICA MOLAR RATIO(8,2)\|MIXED POWDER(8,2)\|PYROXENE(8,2)\|SIEVING(8,2)\|SODIUM CARBONATE POWDER(8,2)\|SYMBOL(8,2)\|TREMOLITE(8,2)\|ULTRASOUND(8,2)\|ALKALI BICARBONATE SOLUTION(8,1)\|ALKALI SOLUBLE IMPURITY(8,1)\|BASIC MAGNESIUM ORTHOSILICATE(8,1)\|BIOMASS DERIVED FUEL(8,1)\|BLUE DIODE(8,1)\|CALCULATION MATRIX(8,1)\|CARBONATABLE SOLID(8,1)\|CARBONATE ION(8,1)\|CARBONATED PRODUCT(8,1)\|CHROMIUM CONTENT(8,1)\|CO2 ATMOSPHERE(8,1)\|CO2 GRAM(8,1)\|COARSE UNREACTED SOLID(8,1)\|COMBINED CO2 QUANTITATIVE DETECTION(8,1)\|COMPRESSIVE LOAD(8,1)\|COOLED PELLET(8,1)\|CRUSHED SAMPLE(8,1)\|CRYSTALLINE COMPOUND(8,1)\|CURING CHAMBER(8,1)\|CYLINDRICAL MOLD(8,1)\|CYLINDRICAL PELLET(8,1)\|DISSOLVED ANION(8,1)\|ESTIMATED MG(8,1)\|GROUND NATURAL TALC(8,1)\|HOT NODULE HEAT(8,1)\|HOT QUENCHED SOLID(8,1)\|INCOMING COMBUSTION AIR PREHEATER(8,1)\|IRON ISOLATION(8,1)\|MAGNESIA FINE PARTICLE(8,1)\|MAGNESIUM SILICATE MINERAL(8,1)\|MAXIMUM CO2 CAPTURE(8,1)\|NATURALLY OCCURRING MINERAL(8,1)\|OUTGOING SOLID PARTICLE(8,1)\|PHASE PROBABILITY(8,1)\|PLUS MAGNESIUM(8,1)\|POROUS BED(8,1)\|POWDER SELF NODULIZE(8,1)\|PREHEATER TOP CYCLONE(8,1)\|PRESSED PELLET(8,1)\|QUALITATIVE PHASE(8,1)\|QUICK WASH(8,1)\|REACTION ESCAPE(8,1)\|REACTOR CONTENT(8,1)\|RED HE NE LASER(8,1)\|RUBBER BOWL(8,1)\|SESQUIHYDRATE(8,1)\|SILICA MOLE(8,1)\|SOLUBLE SALT(8,1)\|SORT REACTION(8,1)\|STEEL CRUCIBLE(8,1)\|SULFUR CONTENT(8,1)\|TREATED SLURRY(8,1)\|WEAK PEAK(8,1)\|XRD DATA RIETVELD ANALYSIS(8,1)\|DEIONIZED WATER(7,5)\|METHYL ISOBUTYL CARBINOL(7,5)\|ALKALI METAL CATION(7,3)\|ATMOSPHERE PRESSURE(7,3)\|DRY CONDITION(7,3)\|FE3O(7,3)\|USEFUL PRODUCT STREAM(7,3)\|NAFEO(7,2)\|SIEVE(7,2)\|4MGO FE2O(6,1)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|AIR BUBBLING(6,1)\|ALKALINE AQUEOUS SOLUTION(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANHYDROUS PRODUCT(6,1)\|ANTIGORITE(6,1)\|AQUEOUS ACID(6,1)\|AQUEOUS PHASE ICP ANALYSIS(6,1)\|AQUEOUS SOLUTION CHEMICAL SPECIES(6,1)\|ATMOSPHERIC PRESSURE CARBONATION(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|CALCINATION(6,1)\|CAO SILICA MOLAR RATIO(6,1)\|CARBONATE PRODUCT(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|CO2 MG(6,1)\|COMPRESSION MACHINE(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|CRYSTALLINE PRODUCT(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|EXCESS FERROUS SULFATE(6,1)\|FAYALITE(6,1)\|FE2SIO(6,1)\|FEO SILICA MOLAR RATIO(6,1)\|FILTER CAKE DRYING(6,1)\|\|(WO2014/082996)\|PRODUCT HECTORITE MANUFACTURER(100,1)\|AMORPHOUS SILICA PRECIPITATE(89,2)\|SILICATE MINERAL TREATMENT(78,2)\|OUTGOING HOT GAS(72,1)\|MOVING GRATE FURNACE(69,2)\|MAGNESIUM SILICATE(65,26)\|OUTGOING HOT SOLID(65,1)\|FORMULA SI(62,2)\|NEUTRALIZATION RATE(61,1)\|CARBONATED SHAPED ARTICLE(59,4)\|THEORETICAL LIMIT(59,1)\|NEUTRALIZING(56,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(55,12)\|COUNTERCURRENT HEAT EXCHANGE EFFICIENCY(54,1)\|INCOMING SOLID(54,1)\|COMPOSITION CARBONATION(53,4)\|GRATE MOVEMENT(51,2)\|GRATE LENGTH(50,1)\|NET ENERGY CONSUMPTION(47,1)\|ALKALI METAL CARBONATE(46,41)\|ALKALI METAL SILICATE(45,11)\|IRON ISOLATION(44,2)\|AMORPHOUS MAGNESIUM SILICATE WATER(42,13)\|EITELITE(41,2)\|COUNTERCURRENT HEAT EXCHANGE(40,3)\|PELLET(39,28)\|FURNACE(39,8)\|GAS LEAVING(36,3)\|MAGNESIUM OXIDE(35,13)\|MOLAR RATIO(34,11)\|MINERAL(33,9)\|INCOMING COMBUSTION AIR(33,2)\|HIGH FREQUENCY INDUCTION FURNACE(32,2)\|ALKALI METAL BICARBONATE(31,4)\|XRAY DIFFRACTION(31,4)\|MAGNESIUM OXIDE MOLAR RATIO(31,1)\|FORMULA OXIDE(30,2)\|MAGNESIUM CARBONATE COMPOUND(28,4)\|FORMULA ALKALI METAL OXIDE(28,2)\|MGC(27,18)\|UNREACTED OLIVINE(27,3)\|ALKALI METAL MAGNESIUM CARBONATE(27,1)\|BED(26,5)\|HEAT TRANSFER EFFICIENCY(25,1)\|PREHEATER CYCLONE TOWER(25,1)\|PLATINUM CRUCIBLE(23,3)\|SOLID PRODUCT(22,7)\|LAB FURNACE(22,4)\|XRAY FLUORESCENCE(22,2)\|HELICOIDAL TEFLON PADDLE(22,1)\|DECARBONATED NODULE(20,1)\|NODULE DEFORMING RISK(20,1)\|OBSCURATION STABILIZATION(20,1)\|MGSI(19,18)\|ROTARY KILN(19,3)\|EARTH CRUST(19,2)\|LASER GRANULOMETRY(19,2)\|OLIVINE SAND(19,2)\|CHROMIUM COMPOUND(18,3)\|EARTH MANTLE MAJORITY(18,1)\|FORSTERITE OLIVINE(18,1)\|MAGNESITE EXPRESSED MGO(18,1)\|SAND FINE GRANULOMETRY(18,1)\|NESQUEHONITE(16,6)\|ANHYDROUS MAGNESIUM SILICATE(16,2)\|CEMENT PLANT(16,2)\|MINERAL SILICATE(16,2)\|CARBON DIOXIDE(15,8)\|ARTINITE(15,5)\|PERICLASE(15,5)\|ENERGY EFFICIENCY(15,3)\|FINE SUSPENSION(15,3)\|CARBONATION REACTION PROGRESS(15,1)\|DISSOLUTION BEHAVIOR(15,1)\|MAGNESIA FINE PARTICLE(15,1)\|MAGNETITE TRACE(15,1)\|MINIATURE FLOTATION CELL(15,1)\|PREHEATER TOWER(15,1)\|REVEALED HYDROMAGNESITE(15,1)\|ROCK ELEMENTAL ANALYSIS(15,1)\|SILICATE HYDROPHOBICITY(15,1)\|ALKALI METAL(14,7)\|BURNING ZONE(14,2)\|DEIONIZED WATER(13,4)\|RICH PRODUCT(13,4)\|BASIC MAGNESIUM ORTHOSILICATE(13,1)\|CARBONATE PARTICLE(13,1)\|COMPANION PELLET(13,1)\|EFFLORESCENCE SAMPLE(13,1)\|IGNITION DATA(13,1)\|LASER GRANULOMETER(13,1)\|MINERAL IMPURITY(13,1)\|NA LEACHING(13,1)\|PERFECTLY BALANCED EQUATION(13,1)\|SAMPLE DEAGGLOMERATION(13,1)\|UNREACTED ANHYDROUS COMPOUND(13,1)\|UNTREATED RESIDUE(13,1)\|02 RICH COMBUSTION(12,2)\|ANHYDROUS MAGNESIUM CARBONATE(12,2)\|CARBOXYMETHYLCELLULOSE(12,2)\|COLORLESS SOLUTION(12,2)\|CRYSTALLINE CONTENT(12,2)\|ESTIMATED MG(12,2)\|GAS ANALYZER(12,2)\|MGO ANHYDROUS PRODUCT(12,2)\|REACTED SAMPLE PHASE CONSTITUTION(12,2)\|STOICHIOMETRIC RATIO(12,2)\|HYDROCYCLONE(11,3)\|ACCRETION FORMATION(11,1)\|AGITATED SUSPENSION(11,1)\|CARBONATE FUSION(11,1)\|CHROMIUM OXIDE(11,1)\|CHROMIUM SELECTIVE SEPARATION(11,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(11,1)\|DECARBONATION REACTION(11,1)\|DRIED HYDROPHASE REACTION(11,1)\|EXCESS COPPERAS(11,1)\|FERMENTATION WASTE GAS(11,1)\|FLOTATION AID(11,1)\|HE NE LASER(11,1)\|HUMAN CARCINOGEN(11,1)\|HYDROMAGNESITE CONCENTRATION(11,1)\|KG FILTER CAKE(11,1)\|LAYERED DOUBLE HYDROXIDE(11,1)\|MINERAL CARBONATE(11,1)\|MINUT ES STIRRING(11,1)\|MOVING GRATE COOLER(11,1)\|NA RECYCLING(11,1)\|NET CONSUMER(11,1)\|PELLET BED(11,1)\|POROUS GLASS FRIT(11,1)\|PRECIPITATED SILICA(11,1)\|PRESSURIZED VESSEL(11,1)\|PURE FORSTERITE(11,1)\|PURE OLIVINE SAMPLE(11,1)\|RAW MAGNESIUM SILICATE(11,1)\|RIETVELD ANALYSIS(11,1)\|SILICATE ANION(11,1)\|SLURRY ADDITIVE(11,1)\|SODIUM SILICATE MILIMOLE LITER(11,1)\|SYNTHETIC HECTORITE(11,1)\|TRISODIUM HYDROGEN DICARBONATE(11,1)\|UNREACTED MAGNESIUM SILICATE(11,1)\|UNREACTED PARTICLE(11,1)\|WATER LEACHING EFFECTIVENESS(11,1)\|WET CARBONATED PELLET(11,1)\|WORK SESSION(11,1)\|HYDROXYCARBONATE WATER(9,4)\|NAFE(9,3)\|ACTINOLITE(9,2)\|AMOSITE(9,2)\|AMPHIBOLE(9,2)\|ANTHOPHYLLITE(9,2)\|BRUCITE(9,2)\|CHRYSOTILE(9,2)\|CONTENT MG(9,2)\|DRIED FILTER(9,2)\|ENSTATITE(9,2)\|HOT GAS PASSAGE(9,2)\|HUMIDITY CONDITION(9,2)\|LIQUID FILTRATE(9,2)\|MAGNESIUM COMPLEX(9,2)\|MG CO2(9,2)\|MIXED POWDER(9,2)\|MOLAR MIXTURE RATIO(9,2)\|PYROXENE(9,2)\|SPECTROMETRY(9,2)\|SYMBOL(9,2)\|TAILING(9,2)\|TREMOLITE(9,2)\|ULTRASOUND(9,2)\|VARIABLE(9,2)\|YELLOW COLORED AQUEOUS PHASE(9,2)\|ALKALI SOLUBLE IMPURITY(9,1)\|ANHYDROUS SODIUM CARBONATE POWDER(9,1)\|AQUEOUS SUSPENSION(9,1)\|AUTOCLAVE HEATING(9,1)\|BALL MILL(9,1)\|BIOMASS DERIVED FUEL(9,1)\|BLUE DIODE(9,1)\|CARBONATABLE SOLID(9,1)\|CARBONATE ION(9,1)\|CARBONATED PRODUCT(9,1)\|CARBONATION REACTION PRODUCT(9,1)\|COARSE UNREACTED SOLID(9,1)\|COMPLETE CARBONATION(9,1)\|CONCENTRATE CONTENT(9,1)\|CRUSHED SAMPLE(9,1)\|CURING CHAMBER(9,1)\|CYLINDRICAL MOLD(9,1)\|CYLINDRICAL PELLET(9,1)\|DETECTED CAKE(9,1)\|DISSOLVED ANION MIXTURE(9,1)\|DRIED MAGNESITE PHASE REACTION(9,1)\|EITELITE PRESENCE(9,1)\|ELECTROCHEMICAL REDUCTION(9,1)\|ENERGY EXPENDITURE(9,1)\|FINAL CARBONATED(9,1)\|FUEL COMBUSTION GAS(9,1)\|GROUND NATURAL TALC(9,1)\|HOT NODULE HEAT(9,1)\|IDEALIZED OVERALL COMPOSITION MG(9,1)\|INTIMATE MIXTURE(9,1)\|IRON QUANTITY(9,1)\|MAGNESITE FORMATION(9,1)\|MAGNESIUM SILICATE MINERAL(9,1)\|MATRIX CALCULATION(9,1)\|MECHANICAL INTEGRITY MAINTENANCE(9,1)\|MECHANICAL STIRRER(9,1)\|MINERAL PREPARATION(9,1)\|MINERAL SEPARATION(9,1)\|NOMINAL COMPOSITION MG(9,1)\|OUTGOING SOLID PARTICLE(9,1)\|PELLET STRENGTH(9,1)\|PLUS MAGNESIUM(9,1)\|POROUS BED(9,1)\|PREHEATER TOP CYCLONE(9,1)\|PREHEATER WALL(9,1)\|QUALITATIVE PHASE(9,1)\|RAPID WASHING(9,1)\|REACTION ESCAPE(9,1)\|REACTION SORT(9,1)\|REMAINDER GIVING(9,1)\|RUBBER BOWL(9,1)\|SESQUIHYDRATE(9,1)\|SI DISSOLUTION(9,1)\|SILICA MOLE(9,1)\|SLURRY SAMPLE(9,1)\|SODIUM HYDROXIDE MILLIMOLE LITER(9,1)\|SOLID FILTER CAKE(9,1)\|STEEL CRUCIBLE(9,1)\|TREATED PELLET(9,1)\|TREATED SLURRY(9,1)\|VENTILATION SPEED(9,1)\|WEAK PEAK(9,1)\|WOOD CHIP(9,1)\|SIEVE(8,2)\|ALKALI METAL CATION(7,3)\|HOT WATER(7,3)\|PRESSURE ATMOSPHERE(7,3)\|ABSORBENT(6,1)\|ABUNDANCE(6,1)\|ALUMINUM(6,1)\|ANALYZING IMAGE(6,1)\|ANTIGORITE(6,1)\|AQUEOUS PHASE ANALYSIS(6,1)\|AQUEOUS SOLUTION PH(6,1)\|ATMOSPHERE ABSOLUTE PRESSURE(6,1)\|ATMOSPHERIC PRESSURE CARBONATION(6,1)\|ATOMIC RATIO(6,1)\|BEAKER(6,1)\|BRONZITE(6,1)\|BUBBLING AIR(6,1)\|CALCINATION(6,1)\|CARBON DIOXIDE EVAPORATION(6,1)\|CATALYST PRESENCE(6,1)\|CHEMICAL ADDITIVE(6,1)\|CHLORITE(6,1)\|CHONDRODITE(6,1)\|CLOSED REACTOR(6,1)\|COMBUSTION EXHAUST GAS(6,1)\|COMPRESSION MACHINE(6,1)\|CONSTANT STIRRING(6,1)\|CRYSTALIZATION(6,1)\|DECAHYDRATE(6,1)\|DECARBONATION DEGREE(6,1)\|DECOMPOSITION(6,1)\|DEW(6,1)\|DIHYDRATE(6,1)\|DIOPSIDE(6,1)\|ELEMENT PERCENTAGE(6,1)\|EXPERIMENT SERIES(6,1)\|FACT VIRTUE(6,1)\|FAYALITE(6,1)\|FILTER CAKE DRYING(6,1)\|FILTER EXPRESSED CAKE(6,1)\|FILTER EXPRESSED MGO(6,1)\|FILTERED SOLID RESIDUE(6,1)\|FINE POWDER(6,1)\|FINE SOLID SUSPENSION(6,1)\|FINENESS(6,1)\|GARNIERITE(6,1)\|GLASS REACTOR(6,1)\|GRANULE(6,1)\|\|(JP2015536897)\|ALKALI METAL(100,81)\|ALKALI METAL CARBONATE(100,46)\|MAGNESIUM(100,16)\|MAGNESIUM OXIDE(100,16)\|ALKALI METAL BICARBONATE(100,6)\|MAGUSHIUMU SILICATE(100,3)\|SILICATE MINERAL(100,3)\|ALKALI METAL ORTHOSILICATE(100,2)\|VIRTUALIZE CARBONATE(34,1)\|SILICA MOLAR RATIO(33,3)\|SOPHORA SOIL(32,5)\|CHROMIUM TKFG(32,1)\|FINE SILICA(29,1)\|MAGNESIUM SILICATE(28,57)\|MAGNESIUM COMPLEX(28,1)\|AMORPHOUS SILICA(25,5)\|ALKALINE AQUEOUS SOLUTION(25,1)\|NEUTRALIZING(25,1)\|CRYSTALIZATION(24,1)\|MOLAR RATIO(22,15)\|MAGNESIUM SILICATE WATER(22,4)\|MOLD GOODS(22,2)\|USABLE PRODUCT(22,1)\|ALKALI METAL SILICATE(21,9)\|AMORPHOUS HYDROUS MAGNESIUM SILICATE(21,9)\|MOVING GRATE(21,2)\|LATTICE(19,1)\|SILICA COMPOUND(18,1)\|MOLDED ARTICLE(17,3)\|PELLET(16,25)\|CO2(16,22)\|MAGNESIA(16,6)\|CHEMICAL FORMULA SILICA(16,2)\|ALKALI METAL BOROHYDRIDE(16,1)\|MAGNESIUM SILICATE ROCK(15,9)\|FIRE(15,1)\|GEL FILTRATION(15,1)\|FURNACE(14,11)\|SOLID PRODUCT(14,9)\|EXPERIMENT(14,5)\|BITTERN OLIVINE(14,3)\|SIO(13,28)\|USEFUL PRODUCT STREAM(13,2)\|ALKALINE METAL CARBONATE(13,1)\|FUME NOBERUJAITO CHONDRO(13,1)\|PRODUCT STREAM(12,6)\|GROUND(11,9)\|FIBROUS SERPENTINE AMPHIBOLE(11,1)\|MAGNESIUM CARBONATE MAGNESIUM CARBONATE TRIHYDRATE(11,1)\|LABORATORY FURNACE(10,4)\|PLATINUM CRUCIBLE(10,3)\|MAGNESIUM CARBONATE HYDROXIDE HYDRATE(10,2)\|GREEN AMPHIBOLE(10,1)\|STONE EITERU SOIL(10,1)\|UNPROCESSED PELLET COMPRESSED PELLET(10,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(9,6)\|COARSE UNREACTED PARTICLE(9,1)\|FULL LENGTH(9,1)\|UNREACTED OLIVINE SAND(9,1)\|WEAK PEAK UNREACTED OLIVINE(9,1)\|CARBONATION REACTION(8,3)\|CHROMIUM COMPOUND(8,2)\|EARTH CRUST(8,2)\|GAS ANALYZER HORIBAEMIA(8,2)\|HYDROGEN DICARBONATE DIHYDRATE(8,1)\|METHANEDIONE NODULE(8,1)\|METHYLISOBUTYLCARBINOL FLOATING AID(8,1)\|OBSCURATION STABILIZATION(8,1)\|SPIRAL PADDLE STIRRER(8,1)\|VAPORIZED METHANEDIONE(8,1)\|CHEMICAL FORMULA(7,6)\|TRUE GROUND(7,3)\|ANHYDROUS MAGNESIUM SILICATE(7,2)\|CAPTURED CO2(7,2)\|NICKEL COMPOUND(7,2)\|PARTICLE SUSPENSION(7,2)\|STRAIGHT AMPHIBOLE(7,2)\|AMORPHOUS SILICA PRECIPITATION(7,1)\|BENEFICIATION SOIL(7,1)\|CARBONATION EXPERIMENT(7,1)\|CHRYSOTILE STONE(7,1)\|COMBUSTION STROKE CO2(7,1)\|DEFORMED NODULE(7,1)\|EXECUTION SUSPENSION PREHEATER(7,1)\|HEAT TRANSFER(7,1)\|HECTORITE LEE HOLDING(7,1)\|METHANEDIONE GAS LIBERATION(7,1)\|OARUNICHI STONE(7,1)\|OEITERU STONE(7,1)\|PREHEATER CYCLONE(7,1)\|ROCK UNREACTED PARTICLE(7,1)\|SILICATE HYDROPHOBICITY(7,1)\|STONE OLIVINE(7,1)\|ULTIMATUM NIGHT(7,1)\|UNREACTED ANHYDROUS COMPOUND(7,1)\|XRD QUALITATIVE PHASE(7,1)\|XRF SPECTROSCOPY(7,1)\|COMBUSTION EXHAUST GAS(6,4)\|HUMIDITY CONDITION(6,4)\|SOLID RESIDUE(6,4)\|IRON COMPOUND(6,2)\|BIOMASS DERIVED FUEL FERMENTATION(6,1)\|BUBBLE CONCENTRATE(6,1)\|DISSOLUTION BEHAVIOR(6,1)\|INORGANIC IMPURITY(6,1)\|LASER MALVERNM(6,1)\|MULTIDISTRIBUTED MATRIX(6,1)\|OLAYERED DOUBLE HYDROXIDE(6,1)\|PELLET HOT ZONE(6,1)\|POWDERED INGREDIENT(6,1)\|PREHEATER CO2(6,1)\|PRESSING IRON CRUCIBLE(6,1)\|SAMPLE DISAGGREGATION(6,1)\|SILICATE DISSOLUTION(6,1)\|SLURRY GASEOUS CO2(6,1)\|STONE LIZARD(6,1)\|TRANSPARENT AMPHIBOLE(6,1)\|REACTION PRODUCT(5,8)\|REACTOR(5,6)\|ASBESTOS(5,3)\|AUTOCLAVE(5,3)\|MAGNESIUM SILICIC ACID(5,3)\|MAGNETITE(5,3)\|BICARBONATE SALT(5,2)\|COMBUSTION ZONE(5,2)\|MAGNESIUM SILICATE MINERAL(5,2)\|MAGNESIUM SODIUM ORTHOSILICATE(5,2)\|STONE SODIUM BICARBONATE(5,2)\|SULFUR CONTENT(5,2)\|AMORPHOUS POLYESTER(5,1)\|CARBONATE DECOMPOSITION(5,1)\|CLAY MINERAL(5,1)\|CO2 DISCHARGE(5,1)\|CO2 LITER(5,1)\|EQUILIBRATED REACTION(5,1)\|ESCAPE REMAINDER(5,1)\|FINE NESS(5,1)\|FLOTATION CELL(5,1)\|GROUND OLIVINE(5,1)\|IRON OLIVINE(5,1)\|LIBERATED CO2(5,1)\|MAGNESIUM MGO(5,1)\|MEASUREMENT REPETITION(5,1)\|MINERAL CARBONATE(5,1)\|MOLDING PELLET(5,1)\|MOVING GRATE FURNACE(5,1)\|OXIDIZATION DECARBURIZATION DEGREE(5,1)\|PELLET CO2(5,1)\|PELLET COMPRESSION(5,1)\|PRINCIPAL CRYSTAL COMPOUND ALKYL(5,1)\|RUBBER BOWL(5,1)\|SLURRY ABSORPTION(5,1)\|SLURRY CO2 REACTION(5,1)\|SYNTHETIC HECTORITE(5,1)\|UNREACTED MAGNESIUM SILICATE(5,1)\|UNTREATED RESIDUE(5,1)\|ALKALI METAL OXIDE(4,7)\|CEMENT PLANT(4,4)\|ROTARY FURNACE(4,4)\|ALKALI METAL HYDROXIDE(4,3)\|ANHYDROUS SODIUM CARBONATE(4,2)\|CARBONATE COMPOUND(4,2)\|CENTRIFUGATION(4,2)\|COLORLESS SOLUTION(4,2)\|CONDITION ADOPTION(4,2)\|ENSTATITE(4,2)\|GRATING(4,2)\|MEASURED LOI DATA(4,2)\|MIXED POWDER(4,2)\|PMGO SIO(4,2)\|RICH PRODUCT(4,2)\|SIEVING(4,2)\|SODIUM CARBONATE HYDRATE POWDER(4,2)\|ALKALI BICARBONATE SOLUTION(4,1)\|ALKALI SOLUBLE IMPURITY(4,1)\|AQUEOUS SOLUTION ANION(4,1)\|ATM CO2(4,1)\|BASIC MAGNESIUM ORTHOSILICATE(4,1)\|BLUE DIODE(4,1)\|BOUND CO2(4,1)\|CALCULATION MATRIX(4,1)\|CARBONATE CO2(4,1)\|CARBONATE ION(4,1)\|CARBONATE PARTICLE(4,1)\|CHIEFLY PRODUCED STONE(4,1)\|CONTAINER PRESSURIZATION(4,1)\|CURING CHAMBER(4,1)\|FILTER CAKE DRIED CO2(4,1)\|FINE SUSPENSION(4,1)\|GAS CO2 CAPTURE(4,1)\|HOT NODULE HEAT(4,1)\|MGSIO4 PENCLASE(4,1)\|MINERAL SEPARATION(4,1)\|MOBILE COOLING(4,1)\|NATURAL TALC PRODUCTION(4,1)\|NODULE GAS(4,1)\|POROUS BED(4,1)\|QUENCHED SAMPLE(4,1)\|RESIDUE NA(4,1)\|SESQUICARBONATE WATER(4,1)\|SILICATE MINERAL TREATMENT(4,1)\|SLURRY RAPID QUENCHING(4,1)\|SODIUM SILICATE MMOLE LITER(4,1)\|SOLID MGO NA(4,1)\|SOLID PRECIPITATE CO2(4,1)\|SOLUBLE SALT(4,1)\|STIRRED SUSPENSION(4,1)\|WHITE DOT(4,1)\|WORK SESSION(4,1)\|XRD RIETVELD ANALYSIS DATA(4,1)\|XRF ANALYSIS(4,1)\|DEIONIZED WATER(3,5)\|HOT GAS(3,3)\|POWDER PRODUCTION(3,3)\|SODIUM OLEATE(3,3)\|THREE DIMENSIONAL WATER(3,3)\|DRYING CONDITION(3,2)\|PELLET BED(3,2)\|ADOPT LIQUID(3,1)\|AGGLOMERATE(3,1)\|ALKALINE SOLUTION(3,1)\|ANHYDROUS ALKALI METAL CARBONATE(3,1)\|ANHYDROUS PRODUCT(3,1)\|ANTIGORITE(3,1)\|BEAKER(3,1)\|BLOWER(3,1)\|BRUCITE(3,1)\|CHLORITE(3,1)\|CHROMIC ACID SALT(3,1)\|CHROMIUM SOLUTION(3,1)\|CLEAR GEL(3,1)\|COMPOSITION FORMULA MG(3,1)\|COMPOSITION VARIABLE(3,1)\|COMPRESSION MACHINE(3,1)\|CONCENTRATION SILICA(3,1)\|COOL SOLID(3,1)\|CYLINDRICAL MOLD(3,1)\|DECAHYDRATE(3,1)\|DEW(3,1)\|DIOPSIDE(3,1)\|DRIED SOLID XRD ANALYSIS(3,1)\|EQUILIBRIUM WATER(3,1)\|EVAPORATION PREVENTION(3,1)\|FILTRATE LIQUID(3,1)\|FINAL SAMPLE NA(3,1)\|FINE POWDER(3,1)\|FINE SOLID(3,1)\|FLOTATION SEPARATION TEST(3,1)\|FORSTERITE(3,1)\|GAMIERITE(3,1)\|GASIFICATION PROCESS CARBONATE(3,1)\|GENERATED CARBONATED PRODUCT(3,1)\|GRANULATOR(3,1)\|GRANULE(3,1)\|HEMATITE(3,1)\|HEMIHYDRATE(3,1)\|\|(CN104812468)\|SILICATE MINERAL(100,3)\|SILICATE MINERAL TREATMENT(100,1)\|FORMULA R2AN(97,3)\|MAGNESIUM SILICATE(81,64)\|AMORPHOUS MAGNESIUM SILICATE(73,7)\|ALKALI METAL CARBONATE(65,51)\|CARBONATED SHAPED ARTICLE(53,2)\|MOLAR RATIO(47,11)\|ALKALI METAL(46,74)\|MAGNESIUM ORTHOSILICATE(43,12)\|CARBONATE COMPOUND(43,2)\|ALKALI METAL SILICATE(40,8)\|ALKALI METAL BICARBONATE(39,5)\|QH2AN OXIDE(39,1)\|MAGNESIUM SILICATE HYDRATE(38,7)\|MAGNESIUM SILICATE ROCK(35,7)\|IRON ISOLATION(34,2)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(33,7)\|MAGNESIUM OXIDE(32,13)\|MAGNESITE TRIHYDRATE(27,4)\|LABORATORY FURNACE PLATINUM CRUCIBLE(24,2)\|MAGNESIUM OXIDE MOLAR RATIO(22,1)\|UNREACTED OLIVINE(20,3)\|EXTRUSION(19,2)\|CARBONATED PELLET(17,2)\|XRF SPECTROSCOPY(17,2)\|2CO3AND METHANEDIONE(15,1)\|AVAILABLEADDITIONAL CO2MAY(15,1)\|DECARBONATED NODULE(15,1)\|WET CARBONATED GRANULE(15,1)\|CHROMIUM COMPOUND(14,2)\|EARTH CRUST(14,2)\|LASER PARTICLE SIZER(14,2)\|OLIVINE SAND(14,2)\|ATMOSPHERE2ALL PELLET(13,1)\|BOUND METHANEDIONE QUANTITATIVE DETECTION(13,1)\|CO2THE NET CONSUMPTION(13,1)\|DAY2UP SKY(13,1)\|MGCO RESPECTIVELY3AND(13,1)\|MITSUBISHIMAGNESIUM ORE(13,1)\|PREHEATER CYCLONE COLUMN(13,1)\|RENDER CARBONATED PARTICLE(13,1)\|MOVING GRATE FURNACE(12,2)\|SLURRY ADDITIVE(12,2)\|ABSORB METHANEDIONE(12,1)\|ALKALI SOLUBLE IMPURITY(12,1)\|AMORPHOUS SILICA PRECIPITATE(12,1)\|CELLTHE STIRRED SUSPENSION(12,1)\|CO2UNDERGOES CURING(12,1)\|GASEOUS CO2 CAPTURE(12,1)\|LEACHING SI CA(12,1)\|METHANEDIONE EVAPORATION(12,1)\|MINERAL CHRYSOTILE(12,1)\|PREHEATER TOWER(12,1)\|SILICATE HYDROPHOBICITY(12,1)\|SODIUM CARBONATECONSISTENT EVAPORATION(12,1)\|UNREACTED ALKALI MAGNESIUM ORTHOSILICATE(12,1)\|SAMPLE REACTION(11,3)\|ASBESTOS(10,4)\|AUTOCLAVE(10,4)\|PERICLASE(10,4)\|POWDERED PRODUCT(10,4)\|WUSTITE(10,4)\|XRD ANALYSIS(10,2)\|CALCIUM FORSTERITE(10,1)\|CARBOXY METHYL CELLULOSE(10,1)\|DISSOLUTION BEHAVIOR(10,1)\|FINE MAGNESITE MG(10,1)\|GASEOUS CO2AND(10,1)\|GASEOUS CO2UP(10,1)\|HYDROMAGNESITE MG(10,1)\|LASER GRANULOMETRY(10,1)\|MAGNESIUM SILICATE RAW MEAL(10,1)\|MICRO FLOTATION(10,1)\|PELLET UPTAKE(10,1)\|PERFECTLY BALANCED EQUATION(10,1)\|RAW MEAL ANALYSIS(10,1)\|ROCK DEPOSIT(10,1)\|SAMPLE DEAGGLOMERATION(10,1)\|SODALITE NA(10,1)\|SODIUM SESQUICARBONATE DIHYDRATE(10,1)\|TRACE IMPURITY(10,1)\|UNREACTED ANHYDROUS COMPOUND(10,1)\|UNTREATED PELLET(10,1)\|UNTREATED RESIDUE(10,1)\|MAGNESIUM SILICATE WATER(9,8)\|ALKALI METAL OXIDE(9,7)\|COMBUSTION ZONE(9,2)\|MAGNESIUM SILICATE MINERAL(9,2)\|SODIUM MAGNESIUM ORTHOSILICATE(9,2)\|FE2O3AND(8,3)\|COLORLESS SOLUTION(8,2)\|ALKALI SILICATE(8,1)\|ANHYDROUS MAGNESIUM SILICATE(8,1)\|CARBONATE EVAPORATION(8,1)\|COARSE UNREACTED SOLID(8,1)\|CONCENTRATE2CO CONTENT(8,1)\|DECARBONATION REACTION(8,1)\|DISPERSIBLE POWDER(8,1)\|FERMENTATION RESIDUE GAS(8,1)\|FLOTATION AID(8,1)\|FORMULA SIO2IS(8,1)\|HYDROMAGNESITE FORMATION(8,1)\|HYDROXY SILICATE(8,1)\|INORGANIC IMPURITY(8,1)\|LAYERED DOUBLE HYDROXIDE(8,1)\|MAGNESIUM REACTION(8,1)\|MATERIAL2ADDITIONAL REACTION(8,1)\|METHANEDIONE GAS RELEASE(8,1)\|MGO SEPARATION(8,1)\|MIE MODEL(8,1)\|MINERAL CARBONATE(8,1)\|MOVING GRATE COOLER(8,1)\|OLIVE SAMPLE(8,1)\|OXIDES2THE MOLAR RATIO(8,1)\|PARTICLE SUSPENSION(8,1)\|POROUS FRIT(8,1)\|PRECIPITATED SILICA(8,1)\|PREHEATER UPPER CYCLONE(8,1)\|RAW MAGNESIUM SILICATE(8,1)\|SILICA MOLE(8,1)\|SILICATE ANION(8,1)\|SODIUM LEACHING(8,1)\|SYNTHETIC HECTORITE(8,1)\|TAILINGS2THE CONTENT(8,1)\|UNREACTED MAGNESIUM SILICATE(8,1)\|UNREACTED PARTICLE(8,1)\|VESSEL PRESSURIZATION(8,1)\|WEATHERED SAMPLE(8,1)\|XH2THE MAGNESIUM SILICATE(8,1)\|SYMBOL(7,3)\|ACTINOLITE(7,2)\|ANHYDROUS SODIUM CARBONATE(7,2)\|BRUCITE(7,2)\|CARBOXYMETHYLCELLULOSE(7,2)\|CENTRIFUGATION(7,2)\|ENSTATITE(7,2)\|GAS STREAM(7,2)\|HYDROCYCLONE(7,2)\|LIQUID FILTRATE(7,2)\|MAGNETITE(7,2)\|MEASURED LOI DATA(7,2)\|MGO SIO2IS(7,2)\|MIXED POWDER(7,2)\|OPACITY(7,2)\|PYROXENE(7,2)\|Q H2O(7,2)\|SODIUM CARBONATE SAMPLE(7,2)\|STEVENSITE(7,2)\|TREMOLITE(7,2)\|ULTRASOUND(7,2)\|3H2O(6,4)\|HOT GAS(6,4)\|MAGNESIUM CARBONATE TRIHYDRATE(6,4)\|METHYL ISOBUTYL CARBINOL(6,4)\|COUNTERCURRENT HEAT EXCHANGE(6,3)\|FOAM(6,2)\|ALKALI CARBONATE COMPOUND(6,1)\|APPLICATIONCONDITION(6,1)\|BASIC CHROMATE(6,1)\|BASIC MAGNESIUM ORTHOSILICATE(6,1)\|BLUE DIODE(6,1)\|CALCULATION MATRIX(6,1)\|CAPTURE2ASSUMING(6,1)\|CARBONATE ION(6,1)\|CARBONATED PRODUCT(6,1)\|CHROMIUM CONTENT(6,1)\|COARSE REACTED SOLID(6,1)\|COMPLEX MAGNESIUM HYDROXY(6,1)\|CRUSHED SAMPLE(6,1)\|CRYSTALLINE COMPOUND(6,1)\|CURING CHAMBER(6,1)\|CYLINDRICAL MOLD(6,1)\|CYLINDRICAL PELLET(6,1)\|DISSOLVED ANION(6,1)\|EFFLORESCENCE(6,1)\|ENHANCE NA(6,1)\|HUMIDITY CONDITION(6,1)\|ICP SOLUTION ANALYSIS(6,1)\|INCOMING COMBUSTION AIR PREHEATER(6,1)\|KILN OUTLET GAS(6,1)\|LITERS2THE GAS BUBBLE(6,1)\|MAGNESIA FINE PARTICLE(6,1)\|MAGNESIUM HYDROXY CARBONATE WATER(6,1)\|MAGNESIUM ORTHOSILICATE COMPOUND(6,1)\|MANTLE2SIO COMPONENT(6,1)\|MIXING PMGO SIO(6,1)\|NA2MGSIO4THE RATIO(6,1)\|NATURALLY OCCURRING MINERAL(6,1)\|ORDINARY STIRRER(6,1)\|PLUS MAGNESIUM(6,1)\|PREDOMINANT PHASE(6,1)\|PREDOMINANT SOLID(6,1)\|QUENCHED HOT SOLID(6,1)\|QUICK WASH(6,1)\|REACTION2TO(6,1)\|REACTOR CONTENT(6,1)\|RED HE NE LASER(6,1)\|RUBBER BOWL(6,1)\|SODALITE FORMATION(6,1)\|SOLID MICROSUSPENSION(6,1)\|SOLUBLE SALT(6,1)\|STEEL CRUCIBLE(6,1)\|SULFUR CONTENT(6,1)\|TRANSPARENT GEL(6,1)\|TREATED SLURRY(6,1)\|TRIHYDRAMAGNESITE(6,1)\|XRD DATA RIETVELD ANALYSIS(6,1)\|XRF ANALYSIS(6,1)\|4H2O(5,3)\|ALKALI METAL CATION(5,3)\|BED(5,3)\|CEMENT PLANT(5,3)\|ROTARY KILN(5,3)\|SODIUM CARBONATE HYDRATE(5,3)\|SODIUM OLEATE(5,3)\|TALC(5,3)\|USEFUL PRODUCT STREAM(5,3)\|WET CONDITION(5,3)\|2CO3MOLAR(5,1)\|2MGSIO4MGO(5,1)\|ABSORBENT(5,1)\|ACIDIC AQUEOUS SOLUTION(5,1)\|ADDED2THEREBY(5,1)\|AGITATION(5,1)\|AGITATOR SPEED(5,1)\|AIR BUBBLING(5,1)\|AMPHIBOLE(5,1)\|ANHYDROUS PRODUCT(5,1)\|ANTIGORITE(5,1)\|AQUEOUS ALKALINE SOLUTION(5,1)\|AQUEOUS PHASE ICP ANALYSIS(5,1)\|ATMOSPHERIC PRESSURE CARBONATION(5,1)\|BAR2WITHOUT(5,1)\|BASIC BICARBONATE SOLUTION(5,1)\|BEAKER(5,1)\|BIOMASS(5,1)\|BRONZITE(5,1)\|CALCINATION(5,1)\|CARBONATE RATIO(5,1)\|CHLORITE(5,1)\|CLOSED REACTOR(5,1)\|COMBUSTION EXHAUST GAS(5,1)\|COMPLEX MIXTURESYNTHETIC METAL(5,1)\|COMPRESSOR(5,1)\|CRYSTALIZATION(5,1)\|CYCLONE SEPARATOR(5,1)\|DECAHYDRATE(5,1)\|DECARBONATION DEGREE(5,1)\|DECOMPOSITION(5,1)\|DEW(5,1)\|DIOPSIDE(5,1)\|DRAINING WATER(5,1)\|DRIED FILTER(5,1)\|DRY POWDER(5,1)\|EXCESS FERROUS SULFATE(5,1)\|EXPERIMENT REACTION PRODUCT(5,1)\|FAYALITE(5,1)\|FILTERED SOLID RESIDUE(5,1)\|FINAL CARBONATED COMPOSITION REMAINS(5,1)\|FINE POWDER(5,1)\|FUEL COMBUSTION GAS(5,1)\|GARNIERITE(5,1)\|GAS ANALYZER(5,1)\|GLASS REACTOR(5,1)\|GRANULATOR(5,1)\|HEMATITE(5,1)\|HORNBLENDE(5,1)\|HOT WATER CIRCULATION(5,1)\|HOT ZONE(5,1)\|HYDRATION(5,1)\|IBALITE(5,1)\|INCORPORATION(5,1)\|\|(CN104812468)\|SILICATE MINERAL TREATMENT(100,2)\|NODULE DISTORTION(92,1)\|FORMULA R2AN(88,3)\|FORMULA SIO2AND(75,1)\|MAGNESIUM SILICATE(69,63)\|AMORPHOUS MAGNESIUM SILICATE(67,7)\|AMORPHOUS SILICA PRECIPITATE(63,2)\|ALKALI METAL CARBONATE(62,52)\|MAGNESIUM SILICATE ROCK(51,7)\|SILICATETHE ACID SALT COMPOUND(48,1)\|MAGNESIUM ORTHOSILICATE(47,14)\|FINENESS(47,1)\|SILICA PRECIPITATE(45,2)\|ALKALI METAL(43,79)\|MOLAR RATIO(43,11)\|ALKALI METAL SILICATE(41,11)\|CARBONATED SHAPED ARTICLE(40,4)\|NEUTRALIZING(39,1)\|QH2AN OXIDE(36,1)\|MAGNESIUM SILICATE HYDRATE(35,7)\|ALKALI METAL BICARBONATE(35,5)\|MAGNESIUM OXIDE(32,16)\|IRON ISOLATION(31,2)\|MOVING GRATE(30,5)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(29,8)\|METHANEDIONE(28,5)\|ACID SALT COMPOUND(26,1)\|PELLET(25,23)\|MAGNESITE TRIHYDRATE(25,4)\|USEFUL PRODUCT(23,3)\|LABORATORY FURNACE PLATINUM CRUCIBLE(22,2)\|LIQUID PRODUCT(21,1)\|FURNACE(20,8)\|MAGNESIUM OXIDE MOLAR RATIO(20,1)\|UNREACTED OLIVINE(19,3)\|STOICHIOMETRIC RATIO(18,2)\|EXTRUSION(16,3)\|REACTION DEGREE(16,2)\|CARBONATED PELLET(15,2)\|VOLUME FRACTION(15,2)\|XRF SPECTROSCOPY(15,2)\|ALKALI METAL PRODUCTION(15,1)\|2CO3AND METHANEDIONE(14,1)\|DECARBONATED NODULE(14,1)\|WET CARBONATED GRANULE(14,1)\|EARTH CRUST(13,2)\|LASER PARTICLE SIZER(13,2)\|OLIVINE SAND(13,2)\|CHROMIUM COMPOUND(12,3)\|ATMOSPHERE2ALL PELLET(12,1)\|BOUND METHANEDIONE QUANTITATIVE DETECTION(12,1)\|CHEMICAL ACTION(12,1)\|CO2THE NET CONSUMPTION(12,1)\|DAY2UP SKY(12,1)\|MGCO RESPECTIVELY3AND(12,1)\|PREHEATER CYCLONE COLUMN(12,1)\|RENDER CARBONATED PARTICLE(12,1)\|UNREACTED RAW MEAL(12,1)\|MOVING GRATE FURNACE(11,2)\|SLURRY ADDITIVE(11,2)\|WUSTITE(10,5)\|SAMPLE REACTION(10,3)\|XRD ANALYSIS(10,2)\|2MGSIO4AND MGO(10,1)\|ABSORB METHANEDIONE(10,1)\|ALKALI SOLUBLE IMPURITY(10,1)\|CO2UNDERGOES CURING(10,1)\|GASEOUS CO2 CAPTURE(10,1)\|HEAT TRANSFER(10,1)\|HORIBA EMIA(10,1)\|HOT WATERTHE HOT JACKET(10,1)\|LEACHING SI CA(10,1)\|METHANEDIONE EVAPORATION(10,1)\|MINERAL CHRYSOTILE(10,1)\|PREHEATER TOWER(10,1)\|PRODUCTONE MANUFACTURER(10,1)\|SILICATE HYDROPHOBICITY(10,1)\|SOLUBLE ONESTHE SALT(10,1)\|UNREACTED ALKALI MAGNESIUM ORTHOSILICATE(10,1)\|ASBESTOS(9,4)\|AUTOCLAVE(9,4)\|PERICLASE(9,4)\|POWDERED PRODUCT(9,4)\|CALCIUM FORSTERITE(9,1)\|CARBOXY METHYL CELLULOSE(9,1)\|DISSOLUTION BEHAVIOR(9,1)\|FINE MAGNESITE MG(9,1)\|GASEOUS CO2AND(9,1)\|GASEOUS CO2UP(9,1)\|HYDROMAGNESITE MG(9,1)\|LASER GRANULOMETRY(9,1)\|MAGNESIUM SILICATE RAW MEAL(9,1)\|MICRO FLOTATION CELL(9,1)\|PELLET UPTAKE(9,1)\|PERFECTLY BALANCED EQUATION(9,1)\|PRESERVEDTHE SAMPLE(9,1)\|RAW MEAL ANALYSIS(9,1)\|ROCK DEPOSIT(9,1)\|SAMPLE DEAGGLOMERATION(9,1)\|SODALITE NA(9,1)\|SODIUM SESQUICARBONATE DIHYDRATE(9,1)\|SUSPENSION PREHEATER(9,1)\|TRACE IMPURITY(9,1)\|UNREACTED ANHYDROUS COMPOUND(9,1)\|UNTREATED PELLET(9,1)\|UNTREATED RESIDUE(9,1)\|MAGNESIUM SILICATE WATER(8,8)\|ALKALI METAL OXIDE(8,7)\|FE2O3AND(8,3)\|MAGNETITE(8,3)\|COMBUSTION ZONE(8,2)\|MAGNESIUM SILICATE MINERAL(8,2)\|SODIUM MAGNESIUM ORTHOSILICATE(8,2)\|COUNTERCURRENT HEAT EXCHANGE(7,4)\|SYMBOL(7,3)\|COLORLESS SOLUTION(7,2)\|ALKALI SILICATE(7,1)\|ANHYDROUS MAGNESIUM SILICATE(7,1)\|CARBONATE EVAPORATION(7,1)\|COARSE UNREACTED SOLID(7,1)\|CONCENTRATE2CO CONTENT(7,1)\|DECARBONATION REACTION(7,1)\|DISPERSIBLE POWDER(7,1)\|FERMENTATION RESIDUE GAS(7,1)\|FLOTATION AID(7,1)\|FORMULA SIO2IS(7,1)\|HYDROMAGNESITE FORMATION(7,1)\|INORGANIC IMPURITY(7,1)\|LAYERED DOUBLE HYDROXIDE(7,1)\|MAGNESIUM REACTION(7,1)\|MATERIAL2ADDITIONAL REACTION(7,1)\|METHANEDIONE GAS RELEASE(7,1)\|MGO SEPARATION(7,1)\|MIE MODEL(7,1)\|MINERAL CARBONATE(7,1)\|MOVING GRATE COOLER(7,1)\|OLIVE SAMPLE(7,1)\|OXIDES2THE MOLAR RATIO(7,1)\|POROUS FRIT(7,1)\|PRECIPITATED SILICA(7,1)\|PREHEATER UPPER CYCLONE(7,1)\|RAW MAGNESIUM SILICATE(7,1)\|SILICA MOLE(7,1)\|SILICATE ANION(7,1)\|SODIUM LEACHING(7,1)\|SYNTHETIC HECTORITE(7,1)\|TAILINGS2THE CONTENT(7,1)\|UNREACTED MAGNESIUM SILICATE(7,1)\|UNREACTED PARTICLE(7,1)\|VESSEL PRESSURIZATION(7,1)\|VIRGIN MAGNESIUM SILICATE(7,1)\|WEATHERED SAMPLE(7,1)\|XH2THE MAGNESIUM SILICATE(7,1)\|3H2O(6,4)\|CEMENT PLANT(6,4)\|MAGNESIUM CARBONATE TRIHYDRATE(6,4)\|ROTARY KILN(6,4)\|ACTINOLITE(6,2)\|ANHYDROUS SODIUM CARBONATE(6,2)\|BRUCITE(6,2)\|CARBOXYMETHYLCELLULOSE(6,2)\|CENTRIFUGATION(6,2)\|ENSTATITE(6,2)\|GAS STREAM(6,2)\|HYDROCYCLONE(6,2)\|LIQUID FILTRATE(6,2)\|MEASURED LOI DATA(6,2)\|MGO SIO2IS(6,2)\|MIXED POWDER(6,2)\|MOLDING(6,2)\|NET ENERGY CONSUMPTION(6,2)\|OPACITY(6,2)\|PYROXENE(6,2)\|Q H2O(6,2)\|SODIUM CARBONATE SAMPLE(6,2)\|STEVENSITE(6,2)\|TREMOLITE(6,2)\|ULTRASOUND(6,2)\|ALKALI CARBONATE COMPOUND(6,1)\|BASIC CHROMATE(6,1)\|BASIC MAGNESIUM ORTHOSILICATE(6,1)\|BLUE DIODE(6,1)\|CALCULATION MATRIX(6,1)\|CAPTURE2ASSUMING(6,1)\|CARBONATE ION(6,1)\|CARBONATED PRODUCT(6,1)\|CHROMIUM CONTENT(6,1)\|CO2MAY(6,1)\|COARSE REACTED SOLID(6,1)\|COMPLEX MAGNESIUM HYDROXY(6,1)\|CRUSHED SAMPLE(6,1)\|CRYSTALLINE COMPOUND(6,1)\|CURING CHAMBER(6,1)\|CYLINDRICAL MOLD(6,1)\|CYLINDRICAL PELLET(6,1)\|DISSOLVED ANION(6,1)\|EFFLORESCENCE(6,1)\|ENHANCE NA(6,1)\|HOUR2THE GAS BUBBLE(6,1)\|HUMIDITY CONDITION(6,1)\|ICP SOLUTION ANALYSIS(6,1)\|INCOMING COMBUSTION AIR PREHEATER(6,1)\|INTERIM2MAY(6,1)\|KILN OUTLET GAS(6,1)\|MAGNESIA FINE PARTICLE(6,1)\|MAGNESIUM HYDROXY CARBONATE WATER(6,1)\|MAGNESIUM ORTHOSILICATE COMPOUND(6,1)\|MANTLE2SIO COMPONENT(6,1)\|MIXING PMGO SIO(6,1)\|NA2MGSIO4THE RATIO(6,1)\|NATURALLY OCCURRING MINERAL(6,1)\|ORDINARY STIRRER(6,1)\|OUTGOING HOT GAS(6,1)\|OUTGOING HOT SOLID(6,1)\|PARTICLE SUSPENSION(6,1)\|PLUS MAGNESIUM(6,1)\|PREDOMINANT PHASE(6,1)\|PREDOMINANT SOLID(6,1)\|QUENCHED HOT SOLID(6,1)\|QUICK WASH(6,1)\|REACTION2TO(6,1)\|REACTOR CONTENT(6,1)\|RED HE NE LASER(6,1)\|RUBBER BOWL(6,1)\|SAMPLEMAGNESITE(6,1)\|SODALITE FORMATION(6,1)\|SOLID MICROSUSPENSION(6,1)\|STEEL CRUCIBLE(6,1)\|STIRRED SUSPENSION(6,1)\|SULFUR CONTENT(6,1)\|TRANSPARENT GEL(6,1)\|TREATED SLURRY(6,1)\|TRIHYDRAMAGNESITE(6,1)\|XRD DATA RIETVELD ANALYSIS(6,1)\|XRF ANALYSIS(6,1)\|METHYL ISOBUTYL CARBINOL(5,4)\|4H2O(5,3)\|ALKALI METAL CATION(5,3)\|BED(5,3)\|SODIUM CARBONATE HYDRATE(5,3)\|SODIUM OLEATE(5,3)\|TALC(5,3)\|USEFUL PRODUCT STREAM(5,3)\|FOAM(5,2)\|2CO3MOLAR(4,1)\|2MGSIO4MGO(4,1)\|ABSORBENT(4,1)\|ACIDIC AQUEOUS SOLUTION(4,1)\|ADDED2THEREBY(4,1)\|AGITATION(4,1)\|AGITATOR SPEED(4,1)\|AIR BUBBLING(4,1)\|AMPHIBOLE(4,1)\|ANHYDROUS PRODUCT(4,1)\|ANTIGORITE(4,1)\|AQUEOUS ALKALINE SOLUTION(4,1)\|AQUEOUS PHASE ICP ANALYSIS(4,1)\|ATMOSPHERIC PRESSURE CARBONATION(4,1)\|BAR2WITHOUT(4,1)\|BASIC BICARBONATE SOLUTION(4,1)\|BEAKER(4,1)\|BIOMASS(4,1)\|BRONZITE(4,1)\|CALCINATION(4,1)\|CARBONATE RATIO(4,1)\|CHLORITE(4,1)\|CLOSED REACTOR(4,1)\|COMBUSTION EXHAUST GAS(4,1)\|COMPRESSOR(4,1)\|CRYSTALIZATION(4,1)\|DECAHYDRATE(4,1)\|DECARBONATION DEGREE(4,1)\|DECOMPOSITION(4,1)\|DEW(4,1)\|DIOPSIDE(4,1)\|DRAINING WATER(4,1)\|DRIED FILTER(4,1)\|DRY POWDER(4,1)\|EXCESS FERROUS SULFATE(4,1)\|EXPERIMENT REACTION PRODUCT(4,1)\|FAYALITE(4,1)\|FILTERED SOLID RESIDUE(4,1)\|FINAL CARBONATED COMPOSITION REMAINS(4,1)\|FINE POWDER(4,1)\|FUEL COMBUSTION GAS(4,1)\|GARNIERITE(4,1)\|GAS ANALYZER(4,1)\|GLASS REACTOR(4,1)\|GRANULATOR(4,1)\|HEMATITE(4,1)\|HORNBLENDE(4,1)\|HOT ZONE(4,1)\|HYDRATION(4,1)\|IBALITE(4,1)\|INCOMING SOLID(4,1)\|INCORPORATION(4,1)\|\|(AU2013351282)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,3)\|SILICATE MINERAL TREATMENT(100,3)\|MAGNESIUM SILICATE(89,63)\|LAFARGE WATERMARK INTELLECTUAL PROPERTY(88,1)\|AMORPHOUS SILICA PRECIPITATE(70,2)\|ALKALI METAL CARBONATE(65,49)\|MAGNESIUM ORTHOSILICATE(63,14)\|SILICA PRECIPITATE(62,1)\|MOLAR RATIO(56,14)\|OUTGOING HOT GAS(56,1)\|MOVING GRATE FURNACE(55,2)\|MAGNESIUM SILICATE HYDRATE(54,6)\|ALKALI METAL SILICATE(53,12)\|ALKALI METAL BICARBONATE(53,5)\|ALKALI METAL(52,76)\|OUTGOING HOT SOLID(51,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(47,12)\|CARBONATED SHAPED ARTICLE(46,4)\|NEUTRALIZING(44,1)\|MAGNESIUM OXIDE(42,16)\|INCOMING SOLID(42,1)\|USEFUL PRODUCT(38,3)\|FURNACE(37,8)\|IRON ISOLATION(35,2)\|MOVING GRATE(34,5)\|INCOMING COMBUSTION AIR(33,1)\|NET ENERGY CONSUMPTION(32,2)\|METHANEDIONE(31,5)\|COUNTERCURRENT HEAT EXCHANGE(31,3)\|TEMPERATURE ELEVATION(31,1)\|PELLET(29,24)\|EITELITE(27,6)\|CO2(25,25)\|AMBIENT TEMPERATURE(25,2)\|MAGNESIUM OXIDE MOLAR RATIO(24,1)\|PTY LTD(23,1)\|SILICON MONOXIDE(23,1)\|MGCO(21,12)\|MOLDING(21,3)\|UNREACTED OLIVINE(21,3)\|COMPLEX ALKALI METAL(21,1)\|BED(20,5)\|HEAT EXCHANGE(19,4)\|PREHEATER CYCLONE TOWER(19,1)\|OLIVINE SAND(18,3)\|PLATINUM CRUCIBLE(18,3)\|SOLID PRODUCT(17,11)\|LAB FURNACE(17,4)\|XRF SPECTROMETRY(17,2)\|PHOTOMETRY HYDROMAGNESITE MG(17,1)\|GASEOUS CO2(15,4)\|HYDROMAGNE SITE(15,3)\|EARTH CRUST(15,2)\|LASER GRANULOMETRY(15,2)\|ASBESTOS FIBRILLAR(15,1)\|DECARBONATED NODULE(15,1)\|OBSCURATION STABILIZATION(15,1)\|NESQUEHONITE(14,7)\|FINE SUSPENSION(14,4)\|CHROMIUM COMPOUND(14,3)\|COUNTER CURRENT HEAT EXCHANGE(14,1)\|DECARBONATED PELLET(14,1)\|FORSTERITE OLIVINE(14,1)\|METHANEDIONE GAS LIBERATION(14,1)\|WET CARBONATED PELLET(14,1)\|ALKALI METAL OXIDE(13,7)\|TAILING(13,6)\|ENERGY EFFICIENCY(12,3)\|SAMPLE REACTION(12,3)\|ANHYDROUS MAGNESIUM SILICATE(12,2)\|SI CA MG(12,2)\|ABSORB METHANEDIONE(12,1)\|DISSOLUTION BEHAVIOR(12,1)\|HEAT TRANSFER(12,1)\|HELICOIDAL TEFLON(12,1)\|HYDRO MAGNESITE(12,1)\|MAGNETITE TRACE(12,1)\|METHANEDIONE EVAPORATION(12,1)\|MINIATURE FLOTATION CELL(12,1)\|PREHEATER TOWER(12,1)\|SILICATE HYDROPHOBICITY(12,1)\|MAGNESIUM SILICATE WATER(11,11)\|EXPERIMENT(11,8)\|AUTOCLAVE(11,5)\|NA2MGSIA(11,5)\|PERICLASE(11,5)\|HUMIDITY CONDITION(11,4)\|BURNING ZONE(11,2)\|FE2O(10,8)\|ANHYDROUS PRODUCT(10,4)\|MG2SIO(10,4)\|PARTICULATE(10,4)\|POWDERED PRODUCT(10,4)\|PRODUCT RICH(10,4)\|R2MGSIO(10,4)\|COLORLESS SOLUTION(10,2)\|ESTIMATED MG(10,2)\|GAS ANALYZER(10,2)\|REACTED SAMPLE PHASE CONSTITUTION(10,2)\|SODIUM MAGNESIUM ORTHOSILICATE(10,2)\|CARBONATE PARTICLE(10,1)\|CO2 UPTAKE(10,1)\|COMPANION PELLET(10,1)\|CONCENTRATE CO2 CONTENT(10,1)\|EFFLORESCENCE SAMPLE(10,1)\|ENHANCE NA RECYCLING(10,1)\|GROUND OLIVINE MIX(10,1)\|LASER GRANULOMETER(10,1)\|NODULE RISK(10,1)\|PERFECTLY BALANCED EQUATION(10,1)\|PRODUCT HECTORITE MANUFACTURER(10,1)\|REACTED SAMPLE OG(10,1)\|SAMPLE DEAGGLOMERATION(10,1)\|SUSPENSION PREHEATER(10,1)\|UNREACTED ANHYDROUS COMPOUND(10,1)\|UNTREATED PELLET(10,1)\|UNTREATED RESIDUE(10,1)\|ALKALINE SOLUTION(9,3)\|COMBUSTION EXHAUST GAS(9,3)\|HYDROCYCLONE(9,3)\|MG2SIA(9,3)\|QUENCHING(9,3)\|REACTION PRODUCT(8,8)\|CARBOXYMETHYLCELLULOSE(8,3)\|ARTINITE MG(8,1)\|CHROMIUM SEPARATION(8,1)\|CO2 EMISSION(8,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(8,1)\|CURING REGIME(8,1)\|DECARBONATION REACTION(8,1)\|DRIED FILTERCAKE(8,1)\|EARTH MANTLE COMPONENT(8,1)\|FERMENTATION RESIDUE GAS(8,1)\|FINE NESS(8,1)\|FINE SAND GRANULOMETRY(8,1)\|FLOTATION AID(8,1)\|HYDROMAGNESITE FORMATION(8,1)\|INORGANIC IMPURITY(8,1)\|LAYERED DOUBLE HYDROXIDE(8,1)\|MINERAL CARBONATE(8,1)\|MOVING GRATE COOLER(8,1)\|NET CONSUMER(8,1)\|OLIVINE SAMPLE(8,1)\|PRECIPITATED SILICA(8,1)\|RAW MAGNESIUM SILICATE(8,1)\|SILICATE ANION(8,1)\|SLURRY CONC(8,1)\|SODIUM SILICATE MILIMOLE LITER(8,1)\|SUSPENSION AGITATION(8,1)\|SYNTHETIC HECTORITE(8,1)\|UNREACTED MAGNESIUM SILICATE(8,1)\|UNREACTED PARTICLE(8,1)\|VESSEL PRESSURIZATION(8,1)\|WORKING SESSION(8,1)\|SODIUM OLEATE(7,5)\|CEMENT PLANT(7,4)\|HOT GAS(7,4)\|HYDROXY CARBONATE WATER(7,4)\|R2SIO(7,4)\|ROTARY KILN(7,4)\|ACTINOLITE(7,2)\|AMOSITE(7,2)\|AMPHIBOLE(7,2)\|ANHYDROUS SODIUM CARBONATE(7,2)\|ANTHOPHYLLITE(7,2)\|BRUCITE(7,2)\|CENTRIFUGATION(7,2)\|CHRYSOTILE(7,2)\|COMPLEX MAGNESIUM(7,2)\|ENSTATITE(7,2)\|FILTER CAKE DRYING(7,2)\|LIQUID FILTRATE(7,2)\|MEASURED LOI DATA(7,2)\|MG094FE(7,2)\|MIXED POWDER(7,2)\|MR2MGSIA(7,2)\|PYROXENE(7,2)\|SIEVING(7,2)\|SODIUM CARBONATE POWDER(7,2)\|SYMBOL(7,2)\|TREMOLITE(7,2)\|ULTRASOUND(7,2)\|ALKALI BICARBONATE SOLUTION(7,1)\|ALKALI SOLUBLE IMPURITY(7,1)\|BASIC MAGNESIUM ORTHOSILICATE(7,1)\|BIOMASS DERIVED FUEL(7,1)\|BLUE DIODE(7,1)\|CALCULATION MATRIX(7,1)\|CARBONATABLE SOLID(7,1)\|CARBONATE ION(7,1)\|CARBONATED PRODUCT(7,1)\|CHROMIUM CONTENT(7,1)\|CO2 ATMOSPHERE(7,1)\|CO2 GRAM(7,1)\|COARSE UNREACTED SOLID(7,1)\|COMBINED CO2 QUANTITATIVE DETECTION(7,1)\|COMPRESSIVE LOAD(7,1)\|COOLED PELLET(7,1)\|CRUSHED SAMPLE(7,1)\|CRYSTALLINE COMPOUND(7,1)\|CRYSTALLINE CONTENT(7,1)\|CURING CHAMBER(7,1)\|CYLINDRICAL MOLD(7,1)\|CYLINDRICAL PELLET(7,1)\|DISSOLVED ANION(7,1)\|DRIED CAKE(7,1)\|EITELITE FORMATION(7,1)\|GROUND NATURAL TALC(7,1)\|HOT NODULE HEAT(7,1)\|HOT QUENCHED SOLID(7,1)\|INCOMING COMBUSTION AIR PREHEATER(7,1)\|MAGNESIA FINE PARTICLE(7,1)\|MAGNESIUM SILICATE MINERAL(7,1)\|MAXIMUM CO2 CAPTURE(7,1)\|MAXIMUM SLURRY ADDITIVE(7,1)\|NATURALLY OCCURRING MINERAL(7,1)\|OUTGOING SOLID PARTICLE(7,1)\|PHASE PROBABILITY(7,1)\|PLUS MAGNESIUM(7,1)\|POROUS BED(7,1)\|POWDER SELF NODULIZE(7,1)\|PREHEATER TOP CYCLONE(7,1)\|PRESSED PELLET(7,1)\|QUALITATIVE PHASE(7,1)\|QUICK WASH(7,1)\|REACTION ESCAPE(7,1)\|REACTOR CONTENT(7,1)\|RED HE NE LASER(7,1)\|RUBBER BOWL(7,1)\|SELFNODULIZATION(7,1)\|SESQUIHYDRATE(7,1)\|SI DISSOLUTION(7,1)\|SILICA MOLE(7,1)\|SOLUBLE SALT(7,1)\|SORT REACTION(7,1)\|STEEL CRUCIBLE(7,1)\|SULFUR CONTENT(7,1)\|TREATED SLURRY(7,1)\|WEAK PEAK(7,1)\|XRD DATA RIETVELD ANALYSIS(7,1)\|DEIONIZED WATER(6,5)\|METHYL ISOBUTYL CARBINOL(6,5)\|ALKALI METAL CATION(6,3)\|ATMOSPHERE PRESSURE(6,3)\|DRY CONDITION(6,3)\|NA2O(6,3)\|USEFUL PRODUCT STREAM(6,3)\|XH2O(6,3)\|NAFEO(6,2)\|SIEVE(6,2)\|ABSORBENT(5,1)\|ABUNDANCE(5,1)\|AIR BUBBLING(5,1)\|ALKALINE AQUEOUS SOLUTION(5,1)\|ALUMINUM(5,1)\|ANALYZING IMAGE(5,1)\|ANTIGORITE(5,1)\|AQUEOUS ACID(5,1)\|AQUEOUS PHASE ICP ANALYSIS(5,1)\|ATMOSPHERIC PRESSURE CARBONATION(5,1)\|BEAKER(5,1)\|BRONZITE(5,1)\|CALCINATION(5,1)\|CARBONATE PRODUCT(5,1)\|CHLORITE(5,1)\|CHONDRODITE(5,1)\|CLOSED REACTOR(5,1)\|COMPRESSION MACHINE(5,1)\|CONSTANT STIRRING(5,1)\|CONTENT MG(5,1)\|CRYSTALIZATION(5,1)\|CRYSTALLINE PHASE(5,1)\|CRYSTALLINE PRODUCT(5,1)\|DECAHYDRATE(5,1)\|DECARBONATION DEGREE(5,1)\|DECOMPOSITION(5,1)\|DEW(5,1)\|DIHYDRATE(5,1)\|DIOPSIDE(5,1)\|EXCESS FERROUS SULFATE(5,1)\|FAYALITE(5,1)\|FE2SIO(5,1)\|FILTER CAKE MG(5,1)\|FILTERED SOLID RESIDUE(5,1)\|FINE POWDER(5,1)\|FUEL COMBUSTION GAS(5,1)\|GARNIERITE(5,1)\|GAS STREAM(5,1)\|GLASS REACTOR(5,1)\|\|(AU2013351282)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,3)\|SILICATE MINERAL TREATMENT(100,3)\|MAGNESIUM SILICATE(89,63)\|LAFARGE WATERMARK INTELLECTUAL PROPERTY(88,1)\|AMORPHOUS SILICA PRECIPITATE(70,2)\|ALKALI METAL CARBONATE(65,49)\|MAGNESIUM ORTHOSILICATE(63,14)\|SILICA PRECIPITATE(62,1)\|MOLAR RATIO(56,14)\|OUTGOING HOT GAS(56,1)\|MOVING GRATE FURNACE(55,2)\|MAGNESIUM SILICATE HYDRATE(54,6)\|ALKALI METAL SILICATE(53,12)\|ALKALI METAL BICARBONATE(53,5)\|ALKALI METAL(52,76)\|OUTGOING HOT SOLID(51,1)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(47,12)\|CARBONATED SHAPED ARTICLE(46,4)\|NEUTRALIZING(44,1)\|MAGNESIUM OXIDE(42,16)\|INCOMING SOLID(42,1)\|USEFUL PRODUCT(38,3)\|FURNACE(37,8)\|IRON ISOLATION(35,2)\|MOVING GRATE(34,5)\|INCOMING COMBUSTION AIR(33,1)\|NET ENERGY CONSUMPTION(32,2)\|METHANEDIONE(31,5)\|COUNTERCURRENT HEAT EXCHANGE(31,3)\|TEMPERATURE ELEVATION(31,1)\|PELLET(29,24)\|EITELITE(27,6)\|CO2(25,25)\|AMBIENT TEMPERATURE(25,2)\|MAGNESIUM OXIDE MOLAR RATIO(24,1)\|PTY LTD(23,1)\|SILICON MONOXIDE(23,1)\|MGCO(21,12)\|MOLDING(21,3)\|UNREACTED OLIVINE(21,3)\|COMPLEX ALKALI METAL(21,1)\|BED(20,5)\|HEAT EXCHANGE(19,4)\|PREHEATER CYCLONE TOWER(19,1)\|OLIVINE SAND(18,3)\|PLATINUM CRUCIBLE(18,3)\|SOLID PRODUCT(17,11)\|LAB FURNACE(17,4)\|XRF SPECTROMETRY(17,2)\|PHOTOMETRY HYDROMAGNESITE MG(17,1)\|GASEOUS CO2(15,4)\|HYDROMAGNE SITE(15,3)\|EARTH CRUST(15,2)\|LASER GRANULOMETRY(15,2)\|ASBESTOS FIBRILLAR(15,1)\|DECARBONATED NODULE(15,1)\|OBSCURATION STABILIZATION(15,1)\|NESQUEHONITE(14,7)\|FINE SUSPENSION(14,4)\|CHROMIUM COMPOUND(14,3)\|COUNTER CURRENT HEAT EXCHANGE(14,1)\|DECARBONATED PELLET(14,1)\|FORSTERITE OLIVINE(14,1)\|METHANEDIONE GAS LIBERATION(14,1)\|WET CARBONATED PELLET(14,1)\|ALKALI METAL OXIDE(13,7)\|TAILING(13,6)\|ENERGY EFFICIENCY(12,3)\|SAMPLE REACTION(12,3)\|ANHYDROUS MAGNESIUM SILICATE(12,2)\|SI CA MG(12,2)\|ABSORB METHANEDIONE(12,1)\|DISSOLUTION BEHAVIOR(12,1)\|HEAT TRANSFER(12,1)\|HELICOIDAL TEFLON(12,1)\|HYDRO MAGNESITE(12,1)\|MAGNETITE TRACE(12,1)\|METHANEDIONE EVAPORATION(12,1)\|MINIATURE FLOTATION CELL(12,1)\|PREHEATER TOWER(12,1)\|SILICATE HYDROPHOBICITY(12,1)\|MAGNESIUM SILICATE WATER(11,11)\|EXPERIMENT(11,8)\|AUTOCLAVE(11,5)\|NA2MGSIA(11,5)\|PERICLASE(11,5)\|HUMIDITY CONDITION(11,4)\|BURNING ZONE(11,2)\|FE2O(10,8)\|ANHYDROUS PRODUCT(10,4)\|MG2SIO(10,4)\|PARTICULATE(10,4)\|POWDERED PRODUCT(10,4)\|PRODUCT RICH(10,4)\|R2MGSIO(10,4)\|COLORLESS SOLUTION(10,2)\|ESTIMATED MG(10,2)\|GAS ANALYZER(10,2)\|REACTED SAMPLE PHASE CONSTITUTION(10,2)\|SODIUM MAGNESIUM ORTHOSILICATE(10,2)\|CARBONATE PARTICLE(10,1)\|CO2 UPTAKE(10,1)\|COMPANION PELLET(10,1)\|CONCENTRATE CO2 CONTENT(10,1)\|EFFLORESCENCE SAMPLE(10,1)\|ENHANCE NA RECYCLING(10,1)\|GROUND OLIVINE MIX(10,1)\|LASER GRANULOMETER(10,1)\|NODULE RISK(10,1)\|PERFECTLY BALANCED EQUATION(10,1)\|PRODUCT HECTORITE MANUFACTURER(10,1)\|REACTED SAMPLE OG(10,1)\|SAMPLE DEAGGLOMERATION(10,1)\|SUSPENSION PREHEATER(10,1)\|UNREACTED ANHYDROUS COMPOUND(10,1)\|UNTREATED PELLET(10,1)\|UNTREATED RESIDUE(10,1)\|ALKALINE SOLUTION(9,3)\|COMBUSTION EXHAUST GAS(9,3)\|HYDROCYCLONE(9,3)\|MG2SIA(9,3)\|QUENCHING(9,3)\|REACTION PRODUCT(8,8)\|CARBOXYMETHYLCELLULOSE(8,3)\|ARTINITE MG(8,1)\|CHROMIUM SEPARATION(8,1)\|CO2 EMISSION(8,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(8,1)\|CURING REGIME(8,1)\|DECARBONATION REACTION(8,1)\|DRIED FILTERCAKE(8,1)\|EARTH MANTLE COMPONENT(8,1)\|FERMENTATION RESIDUE GAS(8,1)\|FINE NESS(8,1)\|FINE SAND GRANULOMETRY(8,1)\|FLOTATION AID(8,1)\|HYDROMAGNESITE FORMATION(8,1)\|INORGANIC IMPURITY(8,1)\|LAYERED DOUBLE HYDROXIDE(8,1)\|MINERAL CARBONATE(8,1)\|MOVING GRATE COOLER(8,1)\|NET CONSUMER(8,1)\|OLIVINE SAMPLE(8,1)\|PRECIPITATED SILICA(8,1)\|RAW MAGNESIUM SILICATE(8,1)\|SILICATE ANION(8,1)\|SLURRY CONC(8,1)\|SODIUM SILICATE MILIMOLE LITER(8,1)\|SUSPENSION AGITATION(8,1)\|SYNTHETIC HECTORITE(8,1)\|UNREACTED MAGNESIUM SILICATE(8,1)\|UNREACTED PARTICLE(8,1)\|VESSEL PRESSURIZATION(8,1)\|WORKING SESSION(8,1)\|SODIUM OLEATE(7,5)\|CEMENT PLANT(7,4)\|HOT GAS(7,4)\|HYDROXY CARBONATE WATER(7,4)\|R2SIO(7,4)\|ROTARY KILN(7,4)\|ACTINOLITE(7,2)\|AMOSITE(7,2)\|AMPHIBOLE(7,2)\|ANHYDROUS SODIUM CARBONATE(7,2)\|ANTHOPHYLLITE(7,2)\|BRUCITE(7,2)\|CENTRIFUGATION(7,2)\|CHRYSOTILE(7,2)\|COMPLEX MAGNESIUM(7,2)\|ENSTATITE(7,2)\|FILTER CAKE DRYING(7,2)\|LIQUID FILTRATE(7,2)\|MEASURED LOI DATA(7,2)\|MG094FE(7,2)\|MIXED POWDER(7,2)\|MR2MGSIA(7,2)\|PYROXENE(7,2)\|SIEVING(7,2)\|SODIUM CARBONATE POWDER(7,2)\|SYMBOL(7,2)\|TREMOLITE(7,2)\|ULTRASOUND(7,2)\|ALKALI BICARBONATE SOLUTION(7,1)\|ALKALI SOLUBLE IMPURITY(7,1)\|BASIC MAGNESIUM ORTHOSILICATE(7,1)\|BIOMASS DERIVED FUEL(7,1)\|BLUE DIODE(7,1)\|CALCULATION MATRIX(7,1)\|CARBONATABLE SOLID(7,1)\|CARBONATE ION(7,1)\|CARBONATED PRODUCT(7,1)\|CHROMIUM CONTENT(7,1)\|CO2 ATMOSPHERE(7,1)\|CO2 GRAM(7,1)\|COARSE UNREACTED SOLID(7,1)\|COMBINED CO2 QUANTITATIVE DETECTION(7,1)\|COMPRESSIVE LOAD(7,1)\|COOLED PELLET(7,1)\|CRUSHED SAMPLE(7,1)\|CRYSTALLINE COMPOUND(7,1)\|CRYSTALLINE CONTENT(7,1)\|CURING CHAMBER(7,1)\|CYLINDRICAL MOLD(7,1)\|CYLINDRICAL PELLET(7,1)\|DISSOLVED ANION(7,1)\|DRIED CAKE(7,1)\|EITELITE FORMATION(7,1)\|GROUND NATURAL TALC(7,1)\|HOT NODULE HEAT(7,1)\|HOT QUENCHED SOLID(7,1)\|INCOMING COMBUSTION AIR PREHEATER(7,1)\|MAGNESIA FINE PARTICLE(7,1)\|MAGNESIUM SILICATE MINERAL(7,1)\|MAXIMUM CO2 CAPTURE(7,1)\|MAXIMUM SLURRY ADDITIVE(7,1)\|NATURALLY OCCURRING MINERAL(7,1)\|OUTGOING SOLID PARTICLE(7,1)\|PHASE PROBABILITY(7,1)\|PLUS MAGNESIUM(7,1)\|POROUS BED(7,1)\|POWDER SELF NODULIZE(7,1)\|PREHEATER TOP CYCLONE(7,1)\|PRESSED PELLET(7,1)\|QUALITATIVE PHASE(7,1)\|QUICK WASH(7,1)\|REACTION ESCAPE(7,1)\|REACTOR CONTENT(7,1)\|RED HE NE LASER(7,1)\|RUBBER BOWL(7,1)\|SELFNODULIZATION(7,1)\|SESQUIHYDRATE(7,1)\|SI DISSOLUTION(7,1)\|SILICA MOLE(7,1)\|SOLUBLE SALT(7,1)\|SORT REACTION(7,1)\|STEEL CRUCIBLE(7,1)\|SULFUR CONTENT(7,1)\|TREATED SLURRY(7,1)\|WEAK PEAK(7,1)\|XRD DATA RIETVELD ANALYSIS(7,1)\|DEIONIZED WATER(6,5)\|METHYL ISOBUTYL CARBINOL(6,5)\|ALKALI METAL CATION(6,3)\|ATMOSPHERE PRESSURE(6,3)\|DRY CONDITION(6,3)\|NA2O(6,3)\|USEFUL PRODUCT STREAM(6,3)\|XH2O(6,3)\|NAFEO(6,2)\|SIEVE(6,2)\|ABSORBENT(5,1)\|ABUNDANCE(5,1)\|AIR BUBBLING(5,1)\|ALKALINE AQUEOUS SOLUTION(5,1)\|ALUMINUM(5,1)\|ANALYZING IMAGE(5,1)\|ANTIGORITE(5,1)\|AQUEOUS ACID(5,1)\|AQUEOUS PHASE ICP ANALYSIS(5,1)\|ATMOSPHERIC PRESSURE CARBONATION(5,1)\|BEAKER(5,1)\|BRONZITE(5,1)\|CALCINATION(5,1)\|CARBONATE PRODUCT(5,1)\|CHLORITE(5,1)\|CHONDRODITE(5,1)\|CLOSED REACTOR(5,1)\|COMPRESSION MACHINE(5,1)\|CONSTANT STIRRING(5,1)\|CONTENT MG(5,1)\|CRYSTALIZATION(5,1)\|CRYSTALLINE PHASE(5,1)\|CRYSTALLINE PRODUCT(5,1)\|DECAHYDRATE(5,1)\|DECARBONATION DEGREE(5,1)\|DECOMPOSITION(5,1)\|DEW(5,1)\|DIHYDRATE(5,1)\|DIOPSIDE(5,1)\|EXCESS FERROUS SULFATE(5,1)\|FAYALITE(5,1)\|FE2SIO(5,1)\|FILTER CAKE MG(5,1)\|FILTERED SOLID RESIDUE(5,1)\|FINE POWDER(5,1)\|FUEL COMBUSTION GAS(5,1)\|GARNIERITE(5,1)\|GAS STREAM(5,1)\|GLASS REACTOR(5,1)\|\|(KR10-2015-0088845)\|SILICATE MINERAL TREATMENT(100,2)\|DEFORMING NODULE(97,1)\|AMORPHOUS SILICA PRECIPITATE(78,1)\|MAGNESIUM SILICATE(72,61)\|AMORPHOUS MAGNESIUM SILICATE(69,6)\|ALKALI METAL CARBONATE(63,47)\|MAGNESIUM SILICATE WEIGHT(54,2)\|CO2ALKALI METAL MAGNESIUM ORTHOSILICATE(53,1)\|MOBILE GRATE(48,3)\|MAGNESIUM ORTHOSILICATE(47,13)\|SILICA PRECIPITATE(45,2)\|ALKALI METAL(43,72)\|CARBONATED SHAPED ARTICLE(43,3)\|MAGNESIUM SILICATE HYDRATE(42,16)\|REACTIVITY(42,1)\|ALKALI METAL SILICATE(41,11)\|MAGNESIUM SILICATE ROCK(39,8)\|NEUTRALIZATION RATE(39,1)\|NEUTRALIZING(39,1)\|CO2ALKALI METAL(37,1)\|HYDRATE(35,7)\|ALKALI METAL BICARBONATE(35,5)\|MAGNESIUM OXIDE(32,17)\|IRON ISOLATION(31,2)\|HUMAN CARCINOGEN(31,1)\|SILICON DIOXIDE(30,4)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(28,10)\|SIO2(27,8)\|INCINERATOR(27,6)\|HEALTH(26,1)\|ASBESTOS(24,4)\|PELLET(23,22)\|LABORATORY INCINERATOR(21,4)\|LIQUID PRODUCT(21,1)\|USEFUL PRODUCT(20,5)\|MAGNESIUM OXIDE MOLAR RATIO(20,1)\|MAGNESIUM CARBONATE COMPOUND(19,3)\|BED(18,5)\|MGO(17,20)\|PREHEATER CYCLONE TOWER(17,1)\|PLATINUM CRUCIBLE(16,3)\|VOLUME FRACTION(15,2)\|XRF SPECTROSCOPY(15,2)\|MOBILE GRATE INCINERATOR(15,1)\|DECARBONATED NODULE(14,1)\|UNREACTED OLIVINE WEAK PEAK(14,1)\|CARBONATION REACTION(13,3)\|OLIVINE SAND(13,2)\|NESQUEHONITE(12,7)\|HYDROXY CARBONATE HYDRATE(12,4)\|CHROMIUM COMPOUND(12,3)\|EARTH MANTLE(12,3)\|RENDER CARBONATED PARTICLE(12,1)\|ANHYDROUS MAGNESIUM SILICATE(11,2)\|CO2 ATM(11,2)\|GASEOUS CO2(11,2)\|HYDROCYCLONE PASSAGE(11,2)\|CARBON DIOXIDE(10,11)\|CARBOXYMETHYLCELLULOSE(10,4)\|MAGNETITE(10,4)\|FINE SUSPENSION(10,3)\|SAMPLE REACTION(10,3)\|BURNING ZONE(10,2)\|CARBONATED MOLDED ARTICLE(10,1)\|HEAT TRANSFER(10,1)\|HYDROMAGNESITE DISSOLVE(10,1)\|PREHEATER TOWER(10,1)\|SERPENTINE CRUSHED SAMPLE(10,1)\|SILICATE HYDROPHOBICITY(10,1)\|AQUEOUS SOLUTION(9,9)\|FERRICLASE(9,4)\|PARTICULATE(9,4)\|ARROW HWASALPYO(9,1)\|BULK UNREACTED ANHYDROUS COMPOUND(9,1)\|DISODIUM BICARBONATE(9,1)\|EARTH OLIVINE(9,1)\|INORGANIC IMPURITY(9,1)\|MAX CO2(9,1)\|PREDOMINANT CRYSTALLINE COMPOUND(9,1)\|RESIDUAL R2C(9,1)\|SAMPLE DEAGGLOMERATION(9,1)\|SERPENTINE CANCER(9,1)\|SI02ALKALI METAL MAGNESIUM ORTHOSILICATE(9,1)\|SILICATE ANION(9,1)\|SUSPENSION PREHEATER(9,1)\|VENTILATION FAN(9,1)\|ALKALI METAL OXIDE(8,7)\|NA2MGSI(8,3)\|SEDIMENTATION(8,3)\|ANHYDROUS MAGNESIUM CARBONATE(8,2)\|CARBONATE MELTING(8,2)\|SODIUM MAGNESIUM ORTHOSILICATE(8,2)\|TOOLIVINE(8,2)\|XRD ANALYSIS(8,2)\|REACTION PRODUCT(7,8)\|10H2THE PEAK(7,1)\|CARBONATE EVAPORATION(7,1)\|CHROMIUM SEPARATION(7,1)\|COMPOSITION MAGNESIUM SILICATE HYDRATE(7,1)\|DISPERSIBLE POWDER(7,1)\|DISSOLUTION BEHAVIOR(7,1)\|DISSOLVE MAGNESIUM SILICATE(7,1)\|FERMENTATION RESIDUE GAS(7,1)\|FINE SAND GRANULOMETRY(7,1)\|FLOATATION AID(7,1)\|IRON OLIVINE(7,1)\|LAYERED DOUBLE HYDROXIDE(7,1)\|MGCO3 ACCOUNT(7,1)\|MINERAL CARBONATE(7,1)\|MOBILE GRATE SPEED(7,1)\|MOVING GRATE FURNACE(7,1)\|NA RECYCLING(7,1)\|NET CONSUMER(7,1)\|OLIVINE SAMPLE(7,1)\|PRECIPITATED SILICA(7,1)\|RAW MAGNESIUM SILICATE(7,1)\|SLURRY ADDITIVE(7,1)\|SPIRAL TEFLON(7,1)\|SUSTAINED STIRRING(7,1)\|SYNTHETIC HECTORITE(7,1)\|UNREACTED MAGNESIUM SILICATE(7,1)\|UNREACTED PARTICLE(7,1)\|UNTREATED RESIDUE(7,1)\|VESSEL PRESSURIZATION(7,1)\|WET CARBONATED PELLET(7,1)\|WHITENED SAMPLE(7,1)\|ALKALI METAL CATION(6,4)\|CEMENT PLANT(6,4)\|COUNTERCURRENT HEAT EXCHANGE(6,4)\|FE2O(6,4)\|ROTARY KILN(6,4)\|ALKALINE SOLUTION(6,2)\|ANHYDROUS SODIUM CARBONATE(6,2)\|ANTHOPHYLLITE(6,2)\|CENTRIFUGATION(6,2)\|CHRYSOTILE(6,2)\|COLORLESS SOLUTION(6,2)\|COMPLEX MAGNESIUM(6,2)\|CRYSTALIZATION(6,2)\|GAS ANALYZER(6,2)\|LIQUID FILTRATE(6,2)\|MEASURED LOI DATA(6,2)\|MIXED POWDER(6,2)\|NET ENERGY CONSUMPTION(6,2)\|QUENCHING(6,2)\|SIEVING(6,2)\|SODIUM CARBONATE HYDRATE POWDER(6,2)\|SODIUM CARBONATE SAMPLE(6,2)\|SYMBOL(6,2)\|ULTRASOUND(6,2)\|ALKALI BICARBONATE SOLUTION(6,1)\|ALKALI SOLUBLE IMPURITY(6,1)\|AUTOCLAVE HEATING(6,1)\|BASIC MAGNESIUM ORTHOSILICATE(6,1)\|BLUE DIODE(6,1)\|CARBONATE ION(6,1)\|CARBONATED PRODUCT(6,1)\|CHROMIUM CONTENT(6,1)\|COARSE PARTIAL REACTION(6,1)\|COUNTER PELLET(6,1)\|CURE CHAMBER(6,1)\|CYLINDRICAL PELLET(6,1)\|DECARBONATION(6,1)\|DRIED FILTER CAKE(6,1)\|EFFLORESCENC(6,1)\|EFFLUENT HOT GAS(6,1)\|FAST CLEANING(6,1)\|FIRING MAGNESIUM CARBONATE(6,1)\|FLOATING CELL(6,1)\|HOT QUENCHED SOLID(6,1)\|HUMIDITY CONDITION(6,1)\|HYDRATION(6,1)\|ICP SOLUTION ANALYSIS(6,1)\|INCOMING COMBUSTION AIR PREHEATER(6,1)\|LOI LOSS(6,1)\|MAGNESIUM SILICATE MINERAL(6,1)\|MAGNESIUM SILICATE SIO2(6,1)\|NA2C03PHILADELPHIA(6,1)\|OUTGOING SOLID PARTICLE(6,1)\|PHASE LIKELIHOOD(6,1)\|POLYDISPERSITY(6,1)\|POROUS BED(6,1)\|POTASSIUM CARBONATE HYDRATE(6,1)\|PREHEATER TOP CYCLONE(6,1)\|QUALITATIVE PHASE(6,1)\|REACTED SAMPLE PHASE CONSTITUTION(6,1)\|REACTOR CONTENT(6,1)\|RED HE NE LASER(6,1)\|RESIDUAL AIR PURGING(6,1)\|RICH COMBUSTION EXHAUST GAS(6,1)\|RUBBER BOWL(6,1)\|SILICA MOLE(6,1)\|SOLID SILICA PRECIPITATE(6,1)\|SPHEROIDIZATION(6,1)\|STEEL CRUCIBLE(6,1)\|STIRRED SUSPENSION(6,1)\|SULFUR CONTENT(6,1)\|TREATED SLURRY(6,1)\|UNTREATED PELLET PAIR(6,1)\|WORKING ZONE(6,1)\|XRD DATA RIETVELD ANALYSIS(6,1)\|POWDER PRODUCTION(5,3)\|SODIUM OLEATE(5,3)\|WET CONDITION(5,3)\|ABSORB CARBON DIOXIDE(4,1)\|ABSORBENT(4,1)\|AIR BUBBLING(4,1)\|AMPHIBITE(4,1)\|ANHYDROUS PRODUCT(4,1)\|ANTIGOLITE(4,1)\|AQUEOUS ALKALI SOLUTION(4,1)\|AQUEOUS PHASE ICP ANALYSIS(4,1)\|ATMOSPHERIC PRESSURE CARBONATION(4,1)\|BEAKER(4,1)\|BICARBONATE MIXED SOLUTION(4,1)\|BRUCITE(4,1)\|CARBON DIOXIDE EVAPORATION(4,1)\|CARBONATE RATIO(4,1)\|CHILLER(4,1)\|CHLORITE(4,1)\|CHONDRODITE(4,1)\|COMPRESSION MACHINE(4,1)\|CONCENTRATE(4,1)\|CYLINDRICAL MOLD(4,1)\|DARKENING(4,1)\|DECAHYDRATE(4,1)\|DECARBOXYLATION DEGREE(4,1)\|DECOMPOSITION(4,1)\|DEW(4,1)\|DRAINING(4,1)\|EFFLUENT HOT SOLID(4,1)\|EITELITE(4,1)\|ENERGY INTENSIVE(4,1)\|ENSTATITE(4,1)\|EXCESS FERROUS SULFATE(4,1)\|EXPERIMENTAL PERIOD(4,1)\|FE2SI(4,1)\|FILTERED SOLID RESIDUE(4,1)\|FINE POWDER(4,1)\|FLOATING TEST(4,1)\|FLOTATION(4,1)\|FUEL COMBUSTION GAS(4,1)\|GARANIERITE(4,1)\|GAS STREAM(4,1)\|GLASS REACTOR(4,1)\|GRANULE(4,1)\|HEAT TREAT PELLET(4,1)\|HEMATITE(4,1)\|HEMICIDE(4,1)\|HEMIHYDRATE(4,1)\|HOT WATER CIRCULATION(4,1)\|HOT ZONE(4,1)\|IDINSITE(4,1)\|IGNITION MEASURED LOSS(4,1)\|INCOMING SOLID(4,1)\|INDUCTION COUPLED PLASMA PHOTOANALYSIS(4,1)\|KAOLIVINE(4,1)\|KILN EXHAUST GAS(4,1)\|LIBERATION(4,1)\|MAGNESIUM HYDROXIDE SEPARATION(4,1)\|MAGNESIUM SILICATE ROCK BACK(4,1)\|\|(CA2892325)\|AMORPHOUS MAGNESIUM SILICATE(100,6)\|SILICATE MINERAL(100,2)\|SILICATE MINERAL TREATMENT(100,2)\|MAGNESIUM SILICATE(84,63)\|AMORPHOUS SILICA PRECIPITATE(70,2)\|MAGNESIUM ORTHOSILICATE(63,14)\|SILICA PRECIPITATE(62,1)\|ALKALI METAL CARBONATE(61,48)\|OUTGOING HOT GAS(56,1)\|MOLAR RATIO(55,15)\|MOVING GRATE FURNACE(55,2)\|MAGNESIUM SILICATE HYDRATE(54,6)\|ALKALI METAL SILICATE(53,12)\|ALKALI METAL BICARBONATE(53,5)\|FORMULA SI(51,1)\|OUTGOING HOT SOLID(51,1)\|ALKALI METAL(50,75)\|ALKALI METAL MAGNESIUM ORTHOSILICATE(47,12)\|CARBONATED SHAPED ARTICLE(46,4)\|NEUTRALIZING(44,1)\|MAGNESIUM OXIDE(42,16)\|INCOMING SOLID(42,1)\|USEFUL PRODUCT(38,3)\|FURNACE(37,8)\|IRON ISOLATION(35,2)\|MOVING GRATE(34,5)\|INCOMING COMBUSTION AIR(33,1)\|NET ENERGY CONSUMPTION(32,2)\|METHANEDIONE(31,5)\|COUNTERCURRENT HEAT EXCHANGE(31,3)\|TEMPERATURE ELEVATION(31,1)\|PELLET(29,24)\|EITELITE(27,5)\|AMBIENT TEMPERATURE(25,2)\|MAGNESIUM OXIDE MOLAR RATIO(24,1)\|MGCO(23,21)\|XH2O(23,1)\|MOLDING(21,3)\|UNREACTED OLIVINE(21,3)\|COMPLEX ALKALI METAL(21,1)\|BED(20,5)\|HEAT EXCHANGE(19,4)\|PREHEATER CYCLONE TOWER(19,1)\|OLIVINE SAND(18,3)\|PLATINUM CRUCIBLE(18,3)\|SOLID PRODUCT(17,11)\|LAB FURNACE(17,4)\|HYDRO MAGNESITE(17,2)\|MGSIA(15,20)\|SLURRY ADDITIVE(15,3)\|LASER GRANULOMETRY(15,2)\|ASBESTOS FIBRILLAR(15,1)\|DECARBONATED NODULE(15,1)\|OBSCURATION STABILIZATION(15,1)\|NESQUEHONITE(14,7)\|FINE SUSPENSION(14,4)\|CHROMIUM COMPOUND(14,3)\|COUNTER CURRENT HEAT EXCHANGE(14,1)\|DECARBONATED PELLET(14,1)\|FORSTERITE OLIVINE(14,1)\|METHANEDIONE GAS LIBERATION(14,1)\|WET CARBONATED PELLET(14,1)\|ALKALI METAL OXIDE(13,7)\|TAILING(13,6)\|EARTH CRUST(13,2)\|SILICON MONOXIDE(12,13)\|EXPERIMENT(12,9)\|ENERGY EFFICIENCY(12,3)\|SAMPLE REACTION(12,3)\|ANHYDROUS MAGNESIUM SILICATE(12,2)\|ABSORB METHANEDIONE(12,1)\|DISSOLUTION BEHAVIOR(12,1)\|HEAT TRANSFER(12,1)\|HELICOIDAL TEFLON(12,1)\|MAGNETITE TRACE(12,1)\|METHANEDIONE EVAPORATION(12,1)\|MINIATURE FLOTATION CELL(12,1)\|PREHEATER TOWER(12,1)\|SILICATE HYDROPHOBICITY(12,1)\|XRF SPECTROMETRY(12,1)\|MAGNESIUM SILICATE WATER(11,11)\|AUTOCLAVE(11,5)\|CONCENTRATE(11,5)\|PERICLASE(11,5)\|HUMIDITY CONDITION(11,4)\|BURNING ZONE(11,2)\|ANHYDROUS PRODUCT(10,4)\|PARTICULATE(10,4)\|POWDERED PRODUCT(10,4)\|PRODUCT RICH(10,4)\|COLORLESS SOLUTION(10,2)\|ESTIMATED MG(10,2)\|GAS ANALYZER(10,2)\|REACTED SAMPLE PHASE CONSTITUTION(10,2)\|RICH COMBUSTION EXHAUST GAS(10,2)\|SODIUM MAGNESIUM ORTHOSILICATE(10,2)\|CARBONATE PARTICLE(10,1)\|COMPANION PELLET(10,1)\|EFFLORESCENCE SAMPLE(10,1)\|EITELITE NA(10,1)\|ENHANCE NA RECYCLING(10,1)\|GROUND OLIVINE MIX(10,1)\|HYDROMAGNESITE MG(10,1)\|LASER GRANULOMETER(10,1)\|NODULE RISK(10,1)\|PERFECTLY BALANCED EQUATION(10,1)\|PRODUCT HECTORITE MANUFACTURER(10,1)\|REACTED SAMPLE OG(10,1)\|SAMPLE DEAGGLOMERATION(10,1)\|SUSPENSION PREHEATER(10,1)\|UNREACTED ANHYDROUS COMPOUND(10,1)\|UNTREATED PELLET(10,1)\|UNTREATED RESIDUE(10,1)\|ALKALINE SOLUTION(9,3)\|FILTER CAKE DRYING(9,3)\|HYDROCYCLONE(9,3)\|QUENCHING(9,3)\|REACTION PRODUCT(8,8)\|CARBOXYMETHYLCELLULOSE(8,3)\|ARTINITE MG(8,1)\|CHROMIUM SEPARATION(8,1)\|COMPOSITION MAGNESIUM SILICATE ROCK(8,1)\|CURING REGIME(8,1)\|DECARBONATION REACTION(8,1)\|DRIED FILTERCAKE(8,1)\|EARTH MANTLE COMPONENT(8,1)\|FERMENTATION RESIDUE GAS(8,1)\|FINE NESS(8,1)\|FINE SAND GRANULOMETRY(8,1)\|FLOTATION AID(8,1)\|HYDROMAGNESITE FORMATION(8,1)\|INORGANIC IMPURITY(8,1)\|LAYERED DOUBLE HYDROXIDE(8,1)\|MINERAL CARBONATE(8,1)\|MOVING GRATE COOLER(8,1)\|NET CONSUMER(8,1)\|OLIVINE SAMPLE(8,1)\|PRECIPITATED SILICA(8,1)\|QUANTITATIVE DETECTION(8,1)\|RAW MAGNESIUM SILICATE(8,1)\|SILICATE ANION(8,1)\|SLURRY CONC(8,1)\|SODIUM SILICATE MILIMOLE LITER(8,1)\|SUSPENSION AGITATION(8,1)\|SYNTHETIC HECTORITE(8,1)\|UNREACTED MAGNESIUM SILICATE(8,1)\|UNREACTED PARTICLE(8,1)\|VESSEL PRESSURIZATION(8,1)\|WORKING SESSION(8,1)\|CEMENT PLANT(7,4)\|HOT GAS(7,4)\|HYDROXY CARBONATE WATER(7,4)\|ROTARY KILN(7,4)\|SODIUM OLEATE(7,4)\|ACTINOLITE(7,2)\|AMOSITE(7,2)\|AMPHIBOLE(7,2)\|ANHYDROUS SODIUM CARBONATE(7,2)\|ANTHOPHYLLITE(7,2)\|BRUCITE(7,2)\|CENTRIFUGATION(7,2)\|CHRYSOTILE(7,2)\|COMPLEX MAGNESIUM(7,2)\|CRYSTALLINE PHASE(7,2)\|ENSTATITE(7,2)\|LIQUID FILTRATE(7,2)\|MEASURED LOI DATA(7,2)\|MG094FE(7,2)\|MIXED POWDER(7,2)\|PYROXENE(7,2)\|SIEVING(7,2)\|SODIUM CARBONATE POWDER(7,2)\|SYMBOL(7,2)\|TREMOLITE(7,2)\|ULTRASOUND(7,2)\|ALKALI BICARBONATE SOLUTION(7,1)\|ALKALI SOLUBLE IMPURITY(7,1)\|BASIC MAGNESIUM ORTHOSILICATE(7,1)\|BIOMASS DERIVED FUEL(7,1)\|BLUE DIODE(7,1)\|CALCULATION MATRIX(7,1)\|CARBONATABLE SOLID(7,1)\|CARBONATE ION(7,1)\|CARBONATED PRODUCT(7,1)\|CHROMIUM CONTENT(7,1)\|COARSE UNREACTED SOLID(7,1)\|COMPRESSIVE LOAD(7,1)\|COOLED PELLET(7,1)\|CRUSHED SAMPLE(7,1)\|CRYSTALLINE COMPOUND(7,1)\|CURING CHAMBER(7,1)\|CYLINDRICAL MOLD(7,1)\|CYLINDRICAL PELLET(7,1)\|DISSOLVED ANION(7,1)\|EITELITE FORMATION(7,1)\|FLOTATION TEST(7,1)\|GASEOUS CO2(7,1)\|GROUND NATURAL TALC(7,1)\|HOT NODULE HEAT(7,1)\|HOT QUENCHED SOLID(7,1)\|INCOMING COMBUSTION AIR PREHEATER(7,1)\|MAGNESIA FINE PARTICLE(7,1)\|MAGNESIUM SILICATE MINERAL(7,1)\|NATURALLY OCCURRING MINERAL(7,1)\|OUTGOING SOLID PARTICLE(7,1)\|PHASE PROBABILITY(7,1)\|PLUS MAGNESIUM(7,1)\|POROUS BED(7,1)\|POWDER SELF NODULIZE(7,1)\|PREHEATER TOP CYCLONE(7,1)\|PRESSED PELLET(7,1)\|QUALITATIVE PHASE(7,1)\|QUICK WASH(7,1)\|REACTION ESCAPE(7,1)\|REACTOR CONTENT(7,1)\|RED HE NE LASER(7,1)\|RUBBER BOWL(7,1)\|SELFNODULIZATION(7,1)\|SESQUIHYDRATE(7,1)\|SI DISSOLUTION(7,1)\|SILICA MOLE(7,1)\|SOLUBLE SALT(7,1)\|SORT REACTION(7,1)\|STEEL CRUCIBLE(7,1)\|SULFUR CONTENT(7,1)\|TREATED SLURRY(7,1)\|WEAK PEAK(7,1)\|XRD DATA RIETVELD ANALYSIS(7,1)\|DEIONIZED WATER(6,5)\|METHYL ISOBUTYL CARBINOL(6,5)\|ALKALI METAL CATION(6,3)\|ATMOSPHERE PRESSURE(6,3)\|DRY CONDITION(6,3)\|MGSIO(6,3)\|USEFUL PRODUCT STREAM(6,3)\|NAFEO(6,2)\|SIEVE(6,2)\|ABSORBENT(5,1)\|ABUNDANCE(5,1)\|AIR BUBBLING(5,1)\|ALKALINE AQUEOUS SOLUTION(5,1)\|ALUMINUM(5,1)\|ANALYZING IMAGE(5,1)\|ANTIGORITE(5,1)\|AQUEOUS ACID(5,1)\|AQUEOUS PHASE ICP ANALYSIS(5,1)\|ATMOSPHERIC PRESSURE CARBONATION(5,1)\|BEAKER(5,1)\|BLOCKAGE(5,1)\|BRONZITE(5,1)\|CALCINATION(5,1)\|CARBONATE PRODUCT(5,1)\|CHLORITE(5,1)\|CHONDRODITE(5,1)\|CLOSED REACTOR(5,1)\|COMPRESSION MACHINE(5,1)\|CONSTANT STIRRING(5,1)\|CRYSTALIZATION(5,1)\|CRYSTALLINE PRODUCT(5,1)\|DECAHYDRATE(5,1)\|DECARBONATION DEGREE(5,1)\|DECOMPOSITION(5,1)\|DEW(5,1)\|DIHYDRATE(5,1)\|DIOPSIDE(5,1)\|DURATIO N(5,1)\|EXCESS FERROUS SULFATE(5,1)\|FAYALITE(5,1)\|FE2SIO(5,1)\|FILTERED SOLID RESIDUE(5,1)\|FINE POWDER(5,1)\|FUEL COMBUSTION GAS(5,1)\|GARNIERITE(5,1)\|GAS STREAM(5,1)\|GLASS REACTOR(5,1)\|GRANULE(5,1)\|HEMATITE(5,1)\|HOT WATER CIRCULATION(5,1)\|	(US9631257)\|The invention claimed is:\|1. A process for the treatment of a silicate mineral, said process comprising:\| preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 600° C. to 1000° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, wherein the reaction is obtained by contacting the alkali metal carbonate compound and the magnesium silicate to each other in a solid state, and\| contacting the first composition with water to produce a second composition comprising an amorphous magnesium silicate hydrate (M-S—H).\|2. A process according to claim 1, wherein M-S—H is represented by an oxide formula in the form pMgO.SiO2.qH2O where p is from 0.5 to 2.0 and q is from 1 to 4.\|3. A process according to claim 1, wherein the magnesium silicate is a magnesium silicate in which the molar ratio of magnesium oxide to silica is from 0.5 to 3.\|4. A process according to claim 1, wherein the magnesium silicate comprises a magnesium silicate rock comprising a magnesium silicate of general composition:\|m(MgO).t(QO).SiO2xH2O\|wherein m is from 0.5 to 3, t is less than or equal to 1, x is from zero to 2, and Q represents a metal or metals other than magnesium.\|5. A process according to claim 4, wherein Q represents iron, nickel and/or chromium which process further comprises isolating an iron, nickel and/or chromium compound.\|6. A process according to claim 1, further comprising isolating or producing magnesium oxide, magnesium hydroxide or an alkali metal silicate from the second composition.\|7. A process according to claim 1, further comprising a step in which the second composition is carbonated to produce a third composition comprising a magnesium carbonate compound.\|8. A process according to the claim 7, further comprising a step in which the magnesium carbonate from the third composition is calcined to produce a fourth composition comprising magnesium oxide.\|9. A process according to claim 7, wherein the carbonation of the second composition is conducted in a second substep, after a first substep during which the second composition is formed by molding or pressing to form a shaped article, such that a carbonated shaped article is obtained.\|10. A process according to claim 1, wherein the temperature is from 800 to 1000° C.	(US9631257)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This is the U.S. National Stage of PCT/EP2013/074732, filed Nov. 26, 2013, which in turn claims priority to European Patent Application No. 12306468.5, filed Nov. 27, 2012 and European Patent Application No. 12306469.3, filed Nov. 27, 2012, the entire contents of these applications are incorporated herein by reference in their entireties.\|(US9631257)\|[0002] This invention relates to a process for the treatment of a silicate mineral. The process uses as starting material a magnesium silicate and produces an anhydrous product comprising an alkali metal magnesium orthosilicate which is then treated with water to obtain a product comprising amorphous magnesium silicate hydrate which can be subjected to further treatments to produce other products.\|[0003] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into common magnesium silicate hydrate minerals such as serpentine (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10(OH)2).\|[0004] Magnesium silicate rocks constitute an excellent source of two important elements, magnesium and silicon, in their oxide forms (MgO and SiO2). Processes to extract these two oxides from such rocks have heretofore been excessively energy-intensive and thus have not been commercialized.\|[0005] Although the magnesium silicate minerals tend to be very “unreactive,” (e.g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a “carbonate fusion”, is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analyzed by standard chemical techniques, thus allowing for total elemental analysis of the rock. The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0006] The term sodium magnesium silicate is sometimes used, in accordance with the International Nomenclature of Cosmetic Ingredients (INCI) to identify synthetic hectorites in the form of nanoparticles and which form clear gels in water. According to one manufacturer of such products hectorites have the formula (Mg5.2Li0.8)(Si8)O20(OH)4Na0.8.\|[0007] The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|[0008] The present invention accordingly provides a process for the preparation of a second composition, said process comprising the steps of:\| - preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 500 to 1200° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, and\| - contacting the first composition with water to produce the second composition comprising an amorphous magnesium silicate hydrate (M-S—H).\|[0011] M-S—H represents an amorphous magnesium silicate hydrate of variable composition. It may be represented by an oxide formula in the form pMgO.SiO2.qH2O where p is typically, from 0.5 to 2.0 and preferably from 0.6 to 1.5; and q is typically from 1 to 4.\|[0012] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate, expressed as silicon dioxide, is preferably from <4:1 to 1:4, more preferably from 3:1 to 1:3, for example 2:1 to 1:2. The ratio is most preferably about 1.\|[0013] The alkali metal is preferably potassium or, more preferably, sodium.\|[0014] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used in the process of the invention.\|[0015] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0016] The magnesium silicate used in the process of the invention is generally a mineral silicate, for example a magnesium silicate rock comprising a magnesium silicate of general composition:\|m(MgO).t(QO).SiO2.xH2O\|wherein m is from 0.5 to 3, t is less than or equal to 1, x is from zero to 2; and Q represents a metal or metals other than magnesium, (for example calcium and/or a transition group metal such as iron, chromium or nickel). Preferably, the magnesium silicate rock comprises 20% or more, more preferably 50% or more of the magnesium silicate of the general composition described hereinbefore. Preferably, when Q represents iron, nickel and/or chromium, the process according to the present invention comprises isolation of an iron, nickel and/or chromium compound\|[0017] It will be understood that the composition or formulae of minerals is often depicted in terms of the theoretical amount of oxides which they contain: the oxides are, however, not present as such in the minerals whose composition is depicted in this way.\|[0018] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc, iddingsite and hectorite. These minerals may contain substantial quantities of iron in addition to magnesium and silicon, and also significant amounts of calcium, aluminium and alkali metals,\|[0019] Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, anthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens. The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0020] The mineral silicate used in the process of the invention is preferably a magnesium silicate. The MgO/SiO2 molar ratio is preferably from 0.5 to 3, more preferably 0.65 to 2. The CaO/SiO2 molar ratio is preferably ≦0.5. The FeO/SiO2 molar ratio is preferably ≦0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≦0.2.\|[0021] The alkali metal carbonate compound used in the process of the invention may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2.2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g. chlorides, sulfates, sulphites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates or hydroxides) are present which, at the temperature used in the process of the invention, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0022] The process of the invention is preferably effected at a temperature from 600 to 1100° C., more preferably from 800 to 1000° C. Heating is generally effected for a few minutes to a few hours.\|[0023] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is solid or liquid.\|[0024] According to a feature of the invention the process is effected at a temperature below the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound.\|[0025] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as “R2O” in which R is as hereinbefore defined present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt.=140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt.=106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0026] The magnesium silicate and alkali metal carbonate compound used in the process of the present invention are preferably in particulate form or in shaped form, e.g. as pellets.\|[0027] Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the process of the invention will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of a fine sand (grain size 0.06 to 0.2 mm) or, if necessary, ground to a fine powder (grain sizes below 0.06 mm). Grain sizes greater than 0.06 mm are generally determined by sieving. Grain sizes lower than 0.06 mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0028] In one embodiment the process of the invention is conducted in a moving grate furnace. This procedure is especially suited to magnesium silicate rocks (rocks comprising mainly MgO and SiO2) in which the MgO/SiO2 molar ratio is close to or greater than 1.\|[0029] A mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in FIG. 1 of the accompanying drawings.\|[0030] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0031] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone (“burning zone”) just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1a) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate (R2CO3):\|Mg2SiO4+R2CO3MgO+R2MgSiO4+CO2↑ (1a)\|in which R is as hereinbefore defined. The more general form of this reaction can be written as in equation (1b) for m>=1 and equation 1(c) for m<1:\|m(MgO).t(QO).SiO2.xH2O+R2CO3(m−1)MgO+R2MgSiO4+tQO+CO2↑+xH2O↑ (1b)\|m(MgO).t(QO).SiO2.xH2O+R2CO3(1−m)R2SiO3+mR2MgSiO4+tQO+CO2↑+xH2O↑ (1c)\|wherein m is greater than or equal to 1 for reaction (1b) and less than or equal to 1 for reaction (1c); and Q, t and x are as hereinbefore defined. The vertical arrows ↑ indicate that the carbon dioxide gas and water vapour produced by this reaction escape from the bed and exits with the rest of the exhaust gases. Thus, ideally, the final solid product remaining in the treated pellets is an intimate mixture comprising an alkali metal magnesium orthosilicate (R2MgSiO4) and optionally either magnesium oxide (MgO, also known as periclase) or an alkali metal silicate (R2SiO3), as well as other solid products comprising the other metals (Q), especially iron, which may present as magnetite (Fe3O4) or possibly as an alkali metal ferrite (RFeO2), calcium, which may be present as silicates, chromium, which may be present as alkali metal chromates (R2CrO4), and nickel, which may be present as oxides.\|[0032] The idealized reactions depicted in equations (1a,b,c) illustrate the production of alkali metal magnesium orthosilicates plus magnesium and/or other oxides and silicates by direct reaction of a stoichiometric (i.e. 1:1R2O:SiO2) mixture of a magnesium silicate and an alkali metal carbonate.\|[0033] This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 3.4 kJ (i.e. about 0.8 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, there will be a significant net energy consumption for the overall process. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0034] In a further embodiment, the process of the invention is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln for the process of the invention which comprises a decarbonation step which produces carbon dioxide.\|[0035] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0036] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 35% of the total solids volume. However, since the reaction itself produces no liquid products (only solids and gases) at the temperatures preferably employed, the risk of the nodules deforming significantly due to melting is quite low even at far higher initial volume fractions of alkali metal carbonate as long as the heating occurs slowly enough to allow for a significant degree of reaction to occur before complete melting of the alkali metal carbonate.\|[0037] According to a further feature of the invention the process of the invention is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The nodules are then decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0038] The decarbonated and cooled pellets or nodules, comprising an alkali metal magnesium orthosilicate and optionally either magnesium oxide or an alkali metal silicate, are treated in order to separate the reaction products.\|[0039] In the process of the invention the first composition, comprising an alkali metal magnesium orthosilicate and optionally either magnesium oxide or alkali metal silicate products is contacted with water to form a second composition comprising solid amorphous magnesium silicate hydrates (and optionally solid magnesium oxide or hydroxide), together with an aqueous solution comprising alkali metal cations, hydroxide anions and silicate anions.\|[0040] The first composition as, for example pellets or nodules, is preferably quenched in an amount of water, such that the final mixture after quenching has a temperature close to, but not exceeding, about 100° C., i.e. enough to quench the solids but avoiding excessive evaporation of water. The hot quenched solids are then preferably crushed and agitated mechanically in the form of a slurry. More water may be added if necessary. Some additional heating may be necessary.\|[0041] Alternatively the treatment with water, for example in the quenching and slurry-formation process described above, can be conducted at a temperature above 100° C. if a pressurized vessel (e.g. an autoclave) is used.\|[0042] Alternatively the above quenching and slurry-formation process can be conducted at lower or ambient temperatures. Water for converting the first composition into the second composition can optionally be recycled from another part of the process.\|[0043] The objective is to separate the components of the second composition by virtue of the facts that (a) alkali metal carbonates, silicates, chromates, sulfates and oxides or hydroxides in the product will tend to dissolve readily in water; (b) alkali metal magnesium orthosilicates will tend to hydrate in hot water to release alkali metals into solution as silicates and hydroxides, the remainder giving a fine suspension of solid amorphous magnesium silicate hydrates, and (c) magnesium oxide (MgO, also known as periclase) in the sample will tend to hydrate in hot water to give magnesium hydroxide (Mg(OH)2, also known as brucite) to form a soft and easily-dispersible powder.\|[0044] The slurry may need to be agitated mechanically. Then, the liquid phase can be separated from the bulk of the unreacted alkali metal magnesium orthosilicate and other unreacted anhydrous compounds, for example by sieving, and the fine particles of magnesium hydroxide and/or amorphous magnesium silicate hydrates which pass through the sieve as a slurry may be separated from the slurry by, for example, filtering, passage through a hydrocyclone, settling and/or centrifuging. The aqueous phase after separation of the magnesium hydroxide comprises an aqueous solution of alkali metal silicates and hydroxides.\|[0045] Alternatively, the separation process may be conducted in two steps, the first step comprising a rapid washing process to remove most of the readily soluble alkali metal carbonates, silicates and hydroxides; and the second step, conducted with additional water, comprising further hydration of both the magnesium oxide and the alkali metal magnesium orthosilicate. In this two-step approach, the water temperature is preferably lower for the first step (for example lower than 60° C.) than for the second step, and an autoclave may be used for the second step if necessary.\|[0046] The overall result of the separation process described above can be summarized as follows:\|[0047] Solid products from the process of the invention, e.g. from the furnace or kiln, (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4, MgO or R2SiO3, QO, and possibly some residual R2CO3) are contacted with water to produce a second composition comprising:\| - (a) a fine suspension comprising amorphous magnesium silicate hydrates and optionally Mg(OH)2 in a highly alkaline solution rich in alkali metal silicates, hydroxides and possibly also carbonates, and\| - (b) coarse unreacted solids comprising R2MgSiO4, and optionally MgO, QO and unreacted particles of the original magnesium silicate rock (e.g. Mg2SiO4), and which separate easily by sedimentation (e.g. in a hydrocyclone) from the fine suspension.\|[0050] The fine suspension can then be further separated (e.g. by filtration) to give\| - (c) fine solids rich in amorphous magnesium silicate hydrates and optionally Mg(OH)2, and\| - (d) a solution rich in alkali metal silicates, hydroxides and possibly also carbonates, and also comprising minor amounts of alkali-soluble impurities, e.g. sulfates and chromates.\|[0053] The initial part of the reaction of the solid products in the process of the invention with water can be written qualitatively as follows, for m≧1 (equation 2a), and m≧1 (equation 2b):\|(m−1)MgO+R2MgSiO4(m−1)Mg(OH)2+“M-S—H”+2R++(OH−,H2SiO4═,CO3═) (2a)\|(1−m)R2SiO3+mR2MgSiO4“M-S—H”+2R++(OH−,H2SiO═,CO3═) (2b)\|[0054] In the above reactions, the main solid compounds produced are an amorphous magnesium silicate hydrate, “M-S—H”, of variable composition, plus, in the case where m>1, magnesium hydroxide (brucite). The alkali metals may dissolve completely in the aqueous phase as alkali metal cations (R+), and the charge of these alkali metal cations is balanced by a mixture of dissolved anions, e.g.: hydroxide (OH−), silicate (H2SiO4═) and possibly also carbonate (CO3═), present in various ratios depending on the conditions and materials used. It is to be understood that equations 2(a) and 2(b) are not perfectly balanced equations but rather are simply intended to indicate the main initial products of the reaction between the solid products of the process of the invention with water.\|[0055] In a further embodiment of the invention the alkaline solution produced in step (d) is contacted with a carbon dioxide-containing gas, for example combustion exhaust gases, to absorb carbon dioxide and yield an alkali metal carbonate, alkali metal bicarbonate or a mixture thereof, generally in solution, and (precipitated) silica.\|[0056] For example, the aqueous solution from step (d) comprising mainly alkali metal hydroxides and silicates and also some residual alkali metal carbonates is contacted with a carbon dioxide-containing gas, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. The solution rapidly absorbs CO2 from such gases to produce a solution of alkali metal carbonates and bicarbonates, and a precipitate of amorphous silica, according to the following, or similar, equations:\|CO2(gas)+2ROH(in solution)R2CO3(in solution) (3)\|CO2(gas)+R2SiO3(in solution)R2CO3(in solution)+SiO2(solid precipitate) (4)\|CO2(gas)+R2CO3(in solution)2RHCO3(in solution) (5)\|[0057] The resulting solid silica precipitate is separated from the solution, for example by filtering, passage through a hydrocyclone, settling and/or centrifuging. In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled. Additional solutes, e.g. known salts, may also be incorporated into the solution. The precipitated silica formed by reaction (4) above can be separated, washed and dried for use in various applications.\|[0058] It will be understood by mass balance that reactions (3) and (4) should in principle be able to absorb essentially all of the CO2 released by the chemical reaction occurring in the process of the invention as shown in reaction (1), but that the additional CO2 resulting from the combustion process required to heat the starting materials will require an additional reaction to absorb it completely, e.g. either a reaction such as (5), or a further reaction with another absorbent.\|[0059] The present invention thus provides a process as described hereinbefore which further comprises isolating or producing magnesium oxide, magnesium hydroxide or an alkali metal silicate from the second composition.\|[0060] In a further embodiment of the invention, the second composition comprising M-S—H is carbonated, i.e. contacted with a carbon dioxide-containing gas, preferably in the presence of water, to produce a third composition comprising a magnesium carbonate compound. The rate of this reaction can be controlled by the temperature, the pressure, the relative humidity, the presence of catalysts and/or the type of reactor used. The carbonation reaction may be represented for example by the equation:\|sCO2(gas)+pMgO.SiO2.qH2Os“MgCO3”+(p−s)MgO.SiO2.q′H2O (6)\|[0061] The first product of this carbonation reaction, shown above as “MgCO3” may be either a simple magnesium carbonate, such as magnesite (MgCO3) or nesquehonite (MgCO3.3H2O), or a complex magnesium hydroxy-carbonate hydrate such as hydromagnesite (Mg(OH)2.4MgCO3.4H2O), or artinite (Mg(OH)2.MgCO3.3H2O), depending on the conditions employed. The second product of this reaction, shown above as “(p−s)MgO.SiO2.q′H2O” represents either an amorphous magnesium silicate hydrate with a lower magnesium/silicon ratio (p−s) than that (p) of the starting magnesium silicate hydrate; or, in the case where p=s, it represents simply a (hydrated) amorphous silica.\|[0062] In a further embodiment of the invention the coarse, partially reacted solids separated from the reaction products in step 1(b) above comprise mainly unreacted magnesium silicate (for example, Mg2SiO4) mixed with some intermediate products (for example, Na2MgSiO4). These can be dried and recycled to be mixed with additional raw magnesium silicate starting material for feeding back into the process. It will be understood that drying should be accomplished in an energy-efficient manner, e.g. first by drainage and then by use of waste heat from the furnace or other sources.\|[0063] According to a further feature of the invention all of the solid products from the process of the invention, e.g. from the furnace or kiln (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4 and MgO or R2SiO3 and/or QO, and possibly some residual R2CO3) are ground together with water to produce a suspension or slurry which is then contacted with a gas containing carbon dioxide, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. During this treatment, in addition to the other reactions described above, (e.g. in equations (2), (3), (4), (5) and (6)), the alkali metal magnesium orthosilicate compound can also react directly with CO2 as indicated by equations (7) and (8) below:\|R2MgSiO4+2CO2MgCO3(solid)+SiO2(solid)+R2CO3(in solution) (7)\|or, alternatively, making use of an alkali bicarbonate solution to achieve the same reaction:\|R2MgSiO4+4RHCO3MgCO3(solid)+SiO2(solid)+3R2CO3(in solution) (8)\|[0064] The alkali metal bicarbonate RHCO3 used in reaction (8) may be formed by the reaction of alkali metal carbonate solution R2CO3 produced in reaction (7) with carbon dioxide, as shown in equation (5).\|[0065] Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300° C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eitelite, Na2CO3.MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|[0066] These types of reaction are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid products. The magnesium carbonate solid produced can be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3.3H2O), or a complex magnesium hydroxy-carbonate hydrate, such as hydromagnesite (Mg(OH)2.4MgCO3.4H2O), or artinite (Mg(OH)2.MgCO3.3H2O), depending on the conditions and starting materials. The silica solid produced can be either a simple amorphous silica or a more complex mixed metal hydroxy-silicate such as an amorphous magnesium silicate hydrate (“M-S—H”). The alkali metal carbonate or bicarbonate solutions resulting from complete carbonation as shown in reactions (3), (4), (5), (7) and (8) can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and then recycled to the start of the process. The solid mixture of magnesium carbonates and silica produced by these reactions is one of the final products of the overall process and, after washing if necessary to recover as much as possible of the soluble alkali metal salts, can be separated for disposal or for use in other processes.\|[0067] The overall object of the process is to convert magnesium silicate rock into useful industrial products with low overall CO2 emissions. A further benefit of the process is to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable mineral carbonate which comprises a magnesium carbonate compound. Below are some examples of some different ways in which the process can be used:\|[0068] Starting with a magnesium silicate rock of composition m(MgO).t(QO).SiO2.xH2O, and recycling substantially all of the alkali metal (R) compounds used back into the process, at least two separate major product streams can be secured from amongst the following:\| - (i) Products rich in magnesium oxide or hydroxide (MgO or Mg(OH)2)\| - (ii) Products rich in amorphous silica (SiO2)\| - (iii) Products rich in amorphous magnesium silicate hydrates (M-S—H)\| - (iv) Products rich in magnesium carbonate compounds, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3, also known as magnesite); or magnesium carbonate trihydrate (MgCO3.3H2O, also known as nesquehonite); or magnesium hydroxy-carbonate hydrate, such as\|[0073] (Mg(OH)2.4MgCO3.4H2O), also known as hydromagnesite, or (Mg(OH)2.MgCO3.3H2O), also known as artinite.\|[0074] Improved separation of the above major solid product streams can also be achieved by the application of other known mineral separation techniques such as, for example, flotation. Such flotation techniques can be effected using flotation aids including sodium oleate, carboxymethylcellulose and methyl isobutyl carbinol.\|[0075] To the extent that CO2 is produced by the combustion of fuels used in the process, e.g. to heat the kiln or furnace, or to dry materials, this CO2 can be captured in the process in the form of product (iv) listed above, by using a treatment process based on the reactions shown above. To the extent that the process is energy-efficient, the aforesaid CO2 produced by the combustion of fuels used in the process, even if substantially completely captured by reactions of the sort shown, for example, in equations (3), (4) and (5), will generally not be sufficient to convert all of the magnesium in the process to product stream (iv), leaving some of the magnesium available for the production of product streams (i) and (iii). However, in another embodiment of the process, additional CO2 can be obtained from other sources and included in the treatment process and thus captured. In such a case, it is possible to operate the process in such a way that product stream (i) is not produced, but the process itself becomes a net consumer of CO2. Moreover, it is also possible to operate the process without separating any of the product streams, so that the only product stream produced is a mixture of some or all of the above product streams\|[0076] In a further approach, the process uses the same magnesium silicate raw material as shown above, but in this case, not all of the alkali metal-rich products of the process are recycled within the process. It is therefore possible to have one or more additional product streams as well as those already listed above. For example, one very useful product stream is an alkali metal silicate, (R2SiO3), either in the form of an alkaline aqueous solution also containing alkali metal hydroxides and/or carbonates, or as a solid product, (for example, obtained by evaporation and/or crystallization).\|[0077] According to a feature of the invention the process further comprises carbonation of the second composition, e.g. by treatment with gases containing CO2, to produce a third composition comprising a magnesium carbonate, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3), also known as magnesite; or magnesium carbonate trihydrate (MgCO3.3H2O), also known as nesquehonite; or magnesium hydroxy-carbonate hydrates, such as (Mg(OH)2.4MgCO3.4H2O), also known as hydromagnesite, or (Mg(OH)2.MgCO3.3H2O), also known as artinite.\|[0078] According to a further feature of the invention, the process further comprises conducting the carbonation of the second composition as described in the preceding paragraph, but where the second composition is first formed by moulding or pressing to form a shaped article, such that the resulting final carbonated composition retains the form of the shaped article but is further hardened by the formation of magnesium carbonates in situ. The present invention thus provides a process as described hereinbefore, in which the carbonation of the second composition is conducted in a second step, after a first step during which the second composition is formed by moulding or pressing to form a shaped article, such that a carbonated shaped article is obtained.\|[0079] The present invention further provides a carbonated shaped article obtained by the process as described hereinbefore.\|[0080] According to a further feature of the invention the process further comprises calcining the magnesium carbonate from the third composition to produce a fourth composition comprising magnesium oxide.\|[0081] The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|[0082] Another useful product stream is rich in transition metal oxides, for example iron oxides such as magnetite (Fe3O4), and which may also contain significant amounts of chromium and/or nickel oxides. These oxides can be concentrated by flotation and/or magnetic separation.\|[0083] Another useful product stream is an alkaline solution containing chromates, which can be treated with a reducing agent and pH control (or by electrochemical reduction) to separate relatively pure chromium oxides, or even chromium metal; for example:\|R2CrO4(aqueous solution)+(reducing agent)Cr(OH)3(solid precipitate)\|[0084] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0085] The term “pellets” as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0086] Particle size distribution when measured by laser granulometry is measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He—Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.\|[0087] The apparatus is checked before each working session by means of a standard sample (Sifraco 010 silica) for which the particle size distribution is known.\|[0088] Measurements are performed with the following parameters: pump speed 2300 rpm and stirrer speed 800 rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30 s (for possible air bubbles to clear), a measurement is carried out for 15 s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0089] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0090] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R, Q, m, t, x and, p are as initially defined.\|[0091] The following non-limiting Examples illustrate embodiments of the invention.\|[0092] The following abbreviations and notations are used:\| - XRF X-ray fluorescence\| - XRD X-ray diffraction\| - ICP Inductively-Coupled Plasma Photometry\| - Hydromagnesite Mg(OH)2.4MgCO3.4H2O\| - Artinite Mg(OH)2.MgCO3.3H2O\| - Eitelite Na2CO3.Mg(CO3)\| - LOI Loss on ignition	(US9631257)\|CROSS-REFERENCE TO RELATED APPLICATIONS\|[0001] This is the U.S. National Stage of PCT/EP2013/074732, filed Nov. 26, 2013, which in turn claims priority to European Patent Application No. 12306468.5, filed Nov. 27, 2012 and European Patent Application No. 12306469.3, filed Nov. 27, 2012, the entire contents of these applications are incorporated herein by reference in their entireties.\|(US9631257)\|[0002] This invention relates to a process for the treatment of a silicate mineral. The process uses as starting material a magnesium silicate and produces an anhydrous product comprising an alkali metal magnesium orthosilicate which is then treated with water to obtain a product comprising amorphous magnesium silicate hydrate which can be subjected to further treatments to produce other products.\|[0003] Magnesium silicate rocks make up the majority of the Earth's mantle, and large surface deposits of such rocks are also found in many locations. The composition of the Earth's mantle is about 70% basic magnesium orthosilicate (Mg2SiO4), and, when this material is found in crystalline form close to the Earth's surface, it is generally in the form of olivine, which is essentially a solid solution between forsterite (pure Mg2SiO4) and fayalite (pure Fe2SiO4), representing the two main components of the Earth's mantle. In the Earth's crust, in addition to olivine, anhydrous magnesium silicates also occur as pyroxenes, such as enstatite (MgSiO3). Due to the action of water, either at the surface or at depth within the Earth's crust, anhydrous magnesium silicates are converted into common magnesium silicate hydrate minerals such as serpentine (with the idealised overall composition Mg3Si2O5(OH)4), and also talc (with the idealised overall composition (Mg3Si4O10(OH)2).\|[0004] Magnesium silicate rocks constitute an excellent source of two important elements, magnesium and silicon, in their oxide forms (MgO and SiO2). Processes to extract these two oxides from such rocks have heretofore been excessively energy-intensive and thus have not been commercialized.\|[0005] Although the magnesium silicate minerals tend to be very “unreactive,” (e.g. in that they have high melting points and also dissolve only very slowly in water or dilute acids), it is known that they will react rapidly with molten alkali metal carbonates, such as sodium carbonate (Na2CO3). Such a process, commonly referred to as a “carbonate fusion”, is often used in the preparation of minerals for chemical analysis. Generally, a large excess of solid alkali metal carbonate (typically at least ten parts of alkali metal carbonate to one part of magnesium silicate rock) is added and the mixture heated to well above the melting point of the alkali metal carbonate. The magnesium silicate completely dissolves in the resulting melt, which after cooling, can easily and rapidly be dissolved in a strong aqueous acid and the solution then analyzed by standard chemical techniques, thus allowing for total elemental analysis of the rock. The carbonate fusion process is a small scale process; it is analytical, not preparative, and is not energy-efficient as it involves melting a large excess of alkali metal carbonate in order to fully dissolve the magnesium silicate.\|[0006] The term sodium magnesium silicate is sometimes used, in accordance with the International Nomenclature of Cosmetic Ingredients (INCI) to identify synthetic hectorites in the form of nanoparticles and which form clear gels in water. According to one manufacturer of such products hectorites have the formula (Mg5.2Li0.8)(Si8)O20(OH)4Na0.8.\|[0007] The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|[0008] The present invention accordingly provides a process for the preparation of a second composition, said process comprising the steps of:\| - preparing a first composition comprising an alkali metal magnesium orthosilicate and optionally either (i) magnesium oxide or (ii) an alkali metal silicate, by reaction, at a temperature from 500 to 1200° C., of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R2O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO2, being from 4:1 to 1:4, and\| - contacting the first composition with water to produce the second composition comprising an amorphous magnesium silicate hydrate (M-S—H).\|[0011] M-S—H represents an amorphous magnesium silicate hydrate of variable composition. It may be represented by an oxide formula in the form pMgO.SiO2.qH2O where p is typically, from 0.5 to 2.0 and preferably from 0.6 to 1.5; and q is typically from 1 to 4.\|[0012] The molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide, to magnesium silicate, expressed as silicon dioxide, is preferably from <4:1 to 1:4, more preferably from 3:1 to 1:3, for example 2:1 to 1:2. The ratio is most preferably about 1.\|[0013] The alkali metal is preferably potassium or, more preferably, sodium.\|[0014] The alkali metal carbonate compound is preferably an alkali metal carbonate. It will be understood that when the alkali metal carbonate compound comprises bicarbonate the latter will generally decompose to the corresponding carbonate at the temperatures used in the process of the invention.\|[0015] The alkali metal carbonate compound may be anhydrous or hydrated. Hydrates of sodium carbonate include the monohydrate and decahydrate. Hydrates of potassium carbonate include the sesquihydrate (also known as hemihydrate). It is preferable, when economically feasible, to use anhydrous alkali metal carbonate compounds to avoid the expenditure of energy required to remove water of hydration.\|[0016] The magnesium silicate used in the process of the invention is generally a mineral silicate, for example a magnesium silicate rock comprising a magnesium silicate of general composition:\|m(MgO).t(QO).SiO2.xH2O\|wherein m is from 0.5 to 3, t is less than or equal to 1, x is from zero to 2; and Q represents a metal or metals other than magnesium, (for example calcium and/or a transition group metal such as iron, chromium or nickel). Preferably, the magnesium silicate rock comprises 20% or more, more preferably 50% or more of the magnesium silicate of the general composition described hereinbefore. Preferably, when Q represents iron, nickel and/or chromium, the process according to the present invention comprises isolation of an iron, nickel and/or chromium compound\|[0017] It will be understood that the composition or formulae of minerals is often depicted in terms of the theoretical amount of oxides which they contain: the oxides are, however, not present as such in the minerals whose composition is depicted in this way.\|[0018] Such minerals include olivines, e.g. forsterite and monticellite; serpentines, e.g. antigorite, chrysotile, lizardite, sepiolite and garnierite; pyroxenes, e.g. enstatite, diopside, bronzite and hypersthene; amphiboles, e.g. amosite, anthophyllite, tremolite and actinolite; humites, e.g. chondrodite and norbergite; and other minerals such as chlorite, talc, iddingsite and hectorite. These minerals may contain substantial quantities of iron in addition to magnesium and silicon, and also significant amounts of calcium, aluminium and alkali metals,\|[0019] Asbestos comprises a group of naturally occurring minerals which includes fibrous serpentine (e.g. chrysotile) and amphibole (e.g. amosite, anthophyllite, tremolite and actinolite) minerals. The fibrillar forms of asbestos are known to be harmful to health and are considered to be human carcinogens. The process of the invention provides a means of converting these minerals into useful (and non-carcinogenic) materials.\|[0020] The mineral silicate used in the process of the invention is preferably a magnesium silicate. The MgO/SiO2 molar ratio is preferably from 0.5 to 3, more preferably 0.65 to 2. The CaO/SiO2 molar ratio is preferably ≦0.5. The FeO/SiO2 molar ratio is preferably ≦0.5. The content of other elements in terms of the (total oxides)/SiO2 molar ratio is preferably ≦0.2.\|[0021] The alkali metal carbonate compound used in the process of the invention may be a mineral, for example trona (tri-sodium hydrogen dicarbonate dihydrate; Na3H(CO3)2.2H2O), or a commercially available compound. It may contain impurities, for example hydroxides and silicates and, generally in smaller amounts, other impurities, e.g. chlorides, sulfates, sulphites, nitrates and nitrites. If impurities (e.g. alkali metal nitrates or hydroxides) are present which, at the temperature used in the process of the invention, decompose to an alkali metal oxide, they should be taken into account when calculating the amount of alkali metal oxide.\|[0022] The process of the invention is preferably effected at a temperature from 600 to 1100° C., more preferably from 800 to 1000° C. Heating is generally effected for a few minutes to a few hours.\|[0023] The process is preferably effected at a temperature at which the magnesium silicate is solid and the alkali metal carbonate corresponding to the alkali metal carbonate compound is solid or liquid.\|[0024] According to a feature of the invention the process is effected at a temperature below the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound.\|[0025] We have found, unexpectedly, that it is possible to obtain a high degree of reaction between an alkali metal carbonate compound, preferably an alkali metal carbonate, and a magnesium silicate when the two materials are contacted with each other in the solid state. They are preferably in particulate form, for example as powders. A mixture of the compounds is preferably heated, for example in a furnace, to a temperature close to, but below, the melting point of the alkali metal carbonate corresponding to the alkali metal compound. The ratio of the carbonate and silicate used is preferably substantially equal to the stoichiometric ratio calculated on the basis that one mole of alkali metal oxide (written generically as “R2O” in which R is as hereinbefore defined present in the alkali metal carbonate compound, is equivalent to one mole of silica (SiO2) present in the magnesium silicate. For example, the stoichiometric mass ratio for the reaction between pure forsterite (Mg2SiO4, mol. wt.=140) and pure anhydrous sodium carbonate (Na2CO3, mol. wt.=106) would be 140:106. It will be understood that the actual silicate and carbonate sources used in practice will not always be pure, but the idealized stoichiometric ratio refers to that in which the heated mixture has an overall molar ratio of R2O:SiO2 substantially equal to unity.\|[0026] The magnesium silicate and alkali metal carbonate compound used in the process of the present invention are preferably in particulate form or in shaped form, e.g. as pellets.\|[0027] Rock used to provide the magnesium silicate and/or alkali metal carbonate compound for the process of the invention will generally be dried, crushed and, if necessary, ground (for example co-ground) to a desired particle size distribution. For example the magnesium silicate may be crushed to the granulometry of a fine sand (grain size 0.06 to 0.2 mm) or, if necessary, ground to a fine powder (grain sizes below 0.06 mm). Grain sizes greater than 0.06 mm are generally determined by sieving. Grain sizes lower than 0.06 mm are generally determined by laser granulometry. Undesirable mineral impurities can be separated to the extent consistent with energy efficiency by mechanical or other separation methods.\|[0028] In one embodiment the process of the invention is conducted in a moving grate furnace. This procedure is especially suited to magnesium silicate rocks (rocks comprising mainly MgO and SiO2) in which the MgO/SiO2 molar ratio is close to or greater than 1.\|[0029] A mixture of alkali metal carbonate compound and magnesium silicate, each in particulate form, is formed into pellets (e.g. using a disc or drum pelletizer). Water may be added to the mixture to facilitate the pelletising process. The pellets are fed onto a moving grate comprising, for example, a high-temperature-resisting steel alloy, where they are heated, for example, by the passage of hot gases, for example fuel combustion gases. The hot gases may be drawn through the bed of pellets on the grate by fans, usually placed under the grate. The process is illustrated diagrammatically in FIG. 1 of the accompanying drawings.\|[0030] Typically, the hot gases are produced by burning, in an excess of air, a fossil fuel, such as natural gas, oil or coal; waste- or biomass-derived fuels, such as wood chips or waste fermentation gases, may also be used. Preferably the fuel used should have a low sulfur content, for example, <1%. The passage of hot gases through the bed heats the particles up, ultimately, to the desired temperature.\|[0031] The rate of heating is controlled, for example, by varying the amount of fuel, the speed of the moving grate and/or the speed of the ventilation fans in order to ensure good overall energy efficiency and also to ensure that the pellets retain their mechanical integrity during the process. The moving grate is designed so that the gases may be passed through the bed several times along the length of the grate to allow for efficient heat transfer between the gases and the pellets, so that the gases leaving the furnace are as cool as possible. Moreover, once the pellets pass through the hottest zone (“burning zone”) just after the combustion of the fuel, they are cooled by passing air through the bed, such that they reach as low a temperature as possible before being discharged from the bed. The incoming air, thus preheated by the outgoing solid particles, is used as the main air supply for combustion of fuel in the burning zone, thus leading to a high overall thermal efficiency for this type of furnace. The theoretical overall chemical reaction occurring during the heating process is shown below in equation (1a) for the reaction between forsterite (Mg2SiO4) and an alkali metal carbonate (R2CO3):\|Mg2SiO4+R2CO3MgO+R2MgSiO4+CO2↑ (1a)\|in which R is as hereinbefore defined. The more general form of this reaction can be written as in equation (1b) for m>=1 and equation 1(c) for m<1:\|m(MgO).t(QO).SiO2.xH2O+R2CO3(m−1)MgO+R2MgSiO4+tQO+CO2↑+xH2O↑ (1b)\|m(MgO).t(QO).SiO2.xH2O+R2CO3(1−m)R2SiO3+mR2MgSiO4+tQO+CO2↑+xH2O↑ (1c)\|wherein m is greater than or equal to 1 for reaction (1b) and less than or equal to 1 for reaction (1c); and Q, t and x are as hereinbefore defined. The vertical arrows ↑ indicate that the carbon dioxide gas and water vapour produced by this reaction escape from the bed and exits with the rest of the exhaust gases. Thus, ideally, the final solid product remaining in the treated pellets is an intimate mixture comprising an alkali metal magnesium orthosilicate (R2MgSiO4) and optionally either magnesium oxide (MgO, also known as periclase) or an alkali metal silicate (R2SiO3), as well as other solid products comprising the other metals (Q), especially iron, which may present as magnetite (Fe3O4) or possibly as an alkali metal ferrite (RFeO2), calcium, which may be present as silicates, chromium, which may be present as alkali metal chromates (R2CrO4), and nickel, which may be present as oxides.\|[0032] The idealized reactions depicted in equations (1a,b,c) illustrate the production of alkali metal magnesium orthosilicates plus magnesium and/or other oxides and silicates by direct reaction of a stoichiometric (i.e. 1:1R2O:SiO2) mixture of a magnesium silicate and an alkali metal carbonate.\|[0033] This type of reaction is very endothermic, mainly due to the liberation of carbon dioxide gas: it consumes about 3.4 kJ (i.e. about 0.8 kcal) of heat per gram of CO2 liberated. Thus, regardless of the temperature at which the reaction is conducted, there will be a significant net energy consumption for the overall process. However, if the reaction is conducted, as described above, in a furnace system which allows for good counter-current heat exchange between the outgoing hot gases and the incoming solids, and likewise between the outgoing hot solids and the incoming combustion air, the net energy consumption can be reduced to a value close to the theoretical limit given above. It is important, for energy efficiency, to have efficient counter-current heat exchange at both the beginning and the end of the process, incoming and outgoing, for example in a moving grate furnace as described above.\|[0034] In a further embodiment, the process of the invention is conducted in a system comprising moving grates for pre-heating and cooling and a rotary kiln for the process of the invention which comprises a decarbonation step which produces carbon dioxide.\|[0035] When a moving grate system is used it is important to maintain the solid in the form of suitably-sized pellets so that they form a porous bed on the grate, allowing for the passage of gases. The pellets preferably retain their mechanical integrity; they preferably also maintain their mean size within pre-determined limits.\|[0036] According to a feature of the invention, in order to facilitate maintenance of the mechanical integrity of the pellets either (a) the maximum solids temperature in the process does not substantially exceed the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, and/or (b) the maximum solid volume fraction of melt-forming material (substantially alkali metal carbonate) in the pellets is generally below the value at which the nodule will deform significantly even if the alkali metal carbonate melts. This value is generally below about 35% of the total solids volume. However, since the reaction itself produces no liquid products (only solids and gases) at the temperatures preferably employed, the risk of the nodules deforming significantly due to melting is quite low even at far higher initial volume fractions of alkali metal carbonate as long as the heating occurs slowly enough to allow for a significant degree of reaction to occur before complete melting of the alkali metal carbonate.\|[0037] According to a further feature of the invention the process of the invention is conducted in a suspension preheater system comprising a plurality of cyclones in a preheater and, for example, a rotary kiln, for example as used in a typical modern cement plant. The starting materials, for example as a mixed substantially dry powder, are fed (cold) into the top cyclone of the preheater. During its passage through the preheater cyclone tower, by counter-current heat exchange with kiln exit gases, the material is heated close to the melting point of the alkali metal carbonate corresponding to the alkali metal carbonate compound, but without reaching this melting point, in order to avoid, for example, the formation of accretions on the walls of the preheater. At the bottom of the preheater tower, the mixed powder enters a rotary kiln in which, as the temperature rises to the melting point of the alkali metal carbonate, the powder self-nodulizes. The ratio of alkali metal carbonate compound to magnesium silicate and/or the particle size distribution of the magnesium silicate and alkali metal carbonate compound in particulate form is chosen to promote self-nodulization. The nodules are then decarbonated in the rotary kiln. The decarbonated nodules are then cooled, for example on a moving grate cooler also as used in typical modern cement plants. The heat of the hot nodules can be used to preheat the incoming combustion air for the kiln by counter-current heat exchange.\|[0038] The decarbonated and cooled pellets or nodules, comprising an alkali metal magnesium orthosilicate and optionally either magnesium oxide or an alkali metal silicate, are treated in order to separate the reaction products.\|[0039] In the process of the invention the first composition, comprising an alkali metal magnesium orthosilicate and optionally either magnesium oxide or alkali metal silicate products is contacted with water to form a second composition comprising solid amorphous magnesium silicate hydrates (and optionally solid magnesium oxide or hydroxide), together with an aqueous solution comprising alkali metal cations, hydroxide anions and silicate anions.\|[0040] The first composition as, for example pellets or nodules, is preferably quenched in an amount of water, such that the final mixture after quenching has a temperature close to, but not exceeding, about 100° C., i.e. enough to quench the solids but avoiding excessive evaporation of water. The hot quenched solids are then preferably crushed and agitated mechanically in the form of a slurry. More water may be added if necessary. Some additional heating may be necessary.\|[0041] Alternatively the treatment with water, for example in the quenching and slurry-formation process described above, can be conducted at a temperature above 100° C. if a pressurized vessel (e.g. an autoclave) is used.\|[0042] Alternatively the above quenching and slurry-formation process can be conducted at lower or ambient temperatures. Water for converting the first composition into the second composition can optionally be recycled from another part of the process.\|[0043] The objective is to separate the components of the second composition by virtue of the facts that (a) alkali metal carbonates, silicates, chromates, sulfates and oxides or hydroxides in the product will tend to dissolve readily in water; (b) alkali metal magnesium orthosilicates will tend to hydrate in hot water to release alkali metals into solution as silicates and hydroxides, the remainder giving a fine suspension of solid amorphous magnesium silicate hydrates, and (c) magnesium oxide (MgO, also known as periclase) in the sample will tend to hydrate in hot water to give magnesium hydroxide (Mg(OH)2, also known as brucite) to form a soft and easily-dispersible powder.\|[0044] The slurry may need to be agitated mechanically. Then, the liquid phase can be separated from the bulk of the unreacted alkali metal magnesium orthosilicate and other unreacted anhydrous compounds, for example by sieving, and the fine particles of magnesium hydroxide and/or amorphous magnesium silicate hydrates which pass through the sieve as a slurry may be separated from the slurry by, for example, filtering, passage through a hydrocyclone, settling and/or centrifuging. The aqueous phase after separation of the magnesium hydroxide comprises an aqueous solution of alkali metal silicates and hydroxides.\|[0045] Alternatively, the separation process may be conducted in two steps, the first step comprising a rapid washing process to remove most of the readily soluble alkali metal carbonates, silicates and hydroxides; and the second step, conducted with additional water, comprising further hydration of both the magnesium oxide and the alkali metal magnesium orthosilicate. In this two-step approach, the water temperature is preferably lower for the first step (for example lower than 60° C.) than for the second step, and an autoclave may be used for the second step if necessary.\|[0046] The overall result of the separation process described above can be summarized as follows:\|[0047] Solid products from the process of the invention, e.g. from the furnace or kiln, (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4, MgO or R2SiO3, QO, and possibly some residual R2CO3) are contacted with water to produce a second composition comprising:\| - (a) a fine suspension comprising amorphous magnesium silicate hydrates and optionally Mg(OH)2 in a highly alkaline solution rich in alkali metal silicates, hydroxides and possibly also carbonates, and\| - (b) coarse unreacted solids comprising R2MgSiO4, and optionally MgO, QO and unreacted particles of the original magnesium silicate rock (e.g. Mg2SiO4), and which separate easily by sedimentation (e.g. in a hydrocyclone) from the fine suspension.\|[0050] The fine suspension can then be further separated (e.g. by filtration) to give\| - (c) fine solids rich in amorphous magnesium silicate hydrates and optionally Mg(OH)2, and\| - (d) a solution rich in alkali metal silicates, hydroxides and possibly also carbonates, and also comprising minor amounts of alkali-soluble impurities, e.g. sulfates and chromates.\|[0053] The initial part of the reaction of the solid products in the process of the invention with water can be written qualitatively as follows, for m≧1 (equation 2a), and m≧1 (equation 2b):\|(m−1)MgO+R2MgSiO4(m−1)Mg(OH)2+“M-S—H”+2R++(OH−,H2SiO4═,CO3═) (2a)\|(1−m)R2SiO3+mR2MgSiO4“M-S—H”+2R++(OH−,H2SiO═,CO3═) (2b)\|[0054] In the above reactions, the main solid compounds produced are an amorphous magnesium silicate hydrate, “M-S—H”, of variable composition, plus, in the case where m>1, magnesium hydroxide (brucite). The alkali metals may dissolve completely in the aqueous phase as alkali metal cations (R+), and the charge of these alkali metal cations is balanced by a mixture of dissolved anions, e.g.: hydroxide (OH−), silicate (H2SiO4═) and possibly also carbonate (CO3═), present in various ratios depending on the conditions and materials used. It is to be understood that equations 2(a) and 2(b) are not perfectly balanced equations but rather are simply intended to indicate the main initial products of the reaction between the solid products of the process of the invention with water.\|[0055] In a further embodiment of the invention the alkaline solution produced in step (d) is contacted with a carbon dioxide-containing gas, for example combustion exhaust gases, to absorb carbon dioxide and yield an alkali metal carbonate, alkali metal bicarbonate or a mixture thereof, generally in solution, and (precipitated) silica.\|[0056] For example, the aqueous solution from step (d) comprising mainly alkali metal hydroxides and silicates and also some residual alkali metal carbonates is contacted with a carbon dioxide-containing gas, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. The solution rapidly absorbs CO2 from such gases to produce a solution of alkali metal carbonates and bicarbonates, and a precipitate of amorphous silica, according to the following, or similar, equations:\|CO2(gas)+2ROH(in solution)R2CO3(in solution) (3)\|CO2(gas)+R2SiO3(in solution)R2CO3(in solution)+SiO2(solid precipitate) (4)\|CO2(gas)+R2CO3(in solution)2RHCO3(in solution) (5)\|[0057] The resulting solid silica precipitate is separated from the solution, for example by filtering, passage through a hydrocyclone, settling and/or centrifuging. In order to avoid an excessively fine amorphous silica precipitate which may cause the solution to gel completely or be too difficult to filter or separate, the concentration, the temperature of the solution during neutralization, and/or the rate of neutralization are controlled. Additional solutes, e.g. known salts, may also be incorporated into the solution. The precipitated silica formed by reaction (4) above can be separated, washed and dried for use in various applications.\|[0058] It will be understood by mass balance that reactions (3) and (4) should in principle be able to absorb essentially all of the CO2 released by the chemical reaction occurring in the process of the invention as shown in reaction (1), but that the additional CO2 resulting from the combustion process required to heat the starting materials will require an additional reaction to absorb it completely, e.g. either a reaction such as (5), or a further reaction with another absorbent.\|[0059] The present invention thus provides a process as described hereinbefore which further comprises isolating or producing magnesium oxide, magnesium hydroxide or an alkali metal silicate from the second composition.\|[0060] In a further embodiment of the invention, the second composition comprising M-S—H is carbonated, i.e. contacted with a carbon dioxide-containing gas, preferably in the presence of water, to produce a third composition comprising a magnesium carbonate compound. The rate of this reaction can be controlled by the temperature, the pressure, the relative humidity, the presence of catalysts and/or the type of reactor used. The carbonation reaction may be represented for example by the equation:\|sCO2(gas)+pMgO.SiO2.qH2Os“MgCO3”+(p−s)MgO.SiO2.q′H2O (6)\|[0061] The first product of this carbonation reaction, shown above as “MgCO3” may be either a simple magnesium carbonate, such as magnesite (MgCO3) or nesquehonite (MgCO3.3H2O), or a complex magnesium hydroxy-carbonate hydrate such as hydromagnesite (Mg(OH)2.4MgCO3.4H2O), or artinite (Mg(OH)2.MgCO3.3H2O), depending on the conditions employed. The second product of this reaction, shown above as “(p−s)MgO.SiO2.q′H2O” represents either an amorphous magnesium silicate hydrate with a lower magnesium/silicon ratio (p−s) than that (p) of the starting magnesium silicate hydrate; or, in the case where p=s, it represents simply a (hydrated) amorphous silica.\|[0062] In a further embodiment of the invention the coarse, partially reacted solids separated from the reaction products in step 1(b) above comprise mainly unreacted magnesium silicate (for example, Mg2SiO4) mixed with some intermediate products (for example, Na2MgSiO4). These can be dried and recycled to be mixed with additional raw magnesium silicate starting material for feeding back into the process. It will be understood that drying should be accomplished in an energy-efficient manner, e.g. first by drainage and then by use of waste heat from the furnace or other sources.\|[0063] According to a further feature of the invention all of the solid products from the process of the invention, e.g. from the furnace or kiln (for example, a mixture of larger particles of unreacted raw materials with R2MgSiO4 and MgO or R2SiO3 and/or QO, and possibly some residual R2CO3) are ground together with water to produce a suspension or slurry which is then contacted with a gas containing carbon dioxide, for example CO2-rich combustion exhaust gases, such as the gases leaving the kiln used to heat-treat the pellets or nodules and those leaving the preheater. During this treatment, in addition to the other reactions described above, (e.g. in equations (2), (3), (4), (5) and (6)), the alkali metal magnesium orthosilicate compound can also react directly with CO2 as indicated by equations (7) and (8) below:\|R2MgSiO4+2CO2MgCO3(solid)+SiO2(solid)+R2CO3(in solution) (7)\|or, alternatively, making use of an alkali bicarbonate solution to achieve the same reaction:\|R2MgSiO4+4RHCO3MgCO3(solid)+SiO2(solid)+3R2CO3(in solution) (8)\|[0064] The alkali metal bicarbonate RHCO3 used in reaction (8) may be formed by the reaction of alkali metal carbonate solution R2CO3 produced in reaction (7) with carbon dioxide, as shown in equation (5).\|[0065] Reactions of the type indicated by equations (7) and (8) may be conducted at ambient temperatures and pressures, or at elevated temperatures and pressures up to as high as 300 atmospheres and 300° C. Additional solid products, such as complex alkali metal magnesium carbonates, (e.g. eitelite, Na2CO3.MgCO3), may form and can be separated, either for re-use within the process or as useful products in their own right.\|[0066] These types of reaction are capable of capturing a large amount of carbon dioxide and converting it into substantially stable solid products. The magnesium carbonate solid produced can be either simple magnesium carbonates, such as magnesite (MgCO3) or nesquehonite (MgCO3.3H2O), or a complex magnesium hydroxy-carbonate hydrate, such as hydromagnesite (Mg(OH)2.4MgCO3.4H2O), or artinite (Mg(OH)2.MgCO3.3H2O), depending on the conditions and starting materials. The silica solid produced can be either a simple amorphous silica or a more complex mixed metal hydroxy-silicate such as an amorphous magnesium silicate hydrate (“M-S—H”). The alkali metal carbonate or bicarbonate solutions resulting from complete carbonation as shown in reactions (3), (4), (5), (7) and (8) can be concentrated, e.g. by evaporation, allowing the solids to be crystallized and then recycled to the start of the process. The solid mixture of magnesium carbonates and silica produced by these reactions is one of the final products of the overall process and, after washing if necessary to recover as much as possible of the soluble alkali metal salts, can be separated for disposal or for use in other processes.\|[0067] The overall object of the process is to convert magnesium silicate rock into useful industrial products with low overall CO2 emissions. A further benefit of the process is to capture gaseous CO2 (e.g. from industrial flue gases) and convert it into a substantially stable mineral carbonate which comprises a magnesium carbonate compound. Below are some examples of some different ways in which the process can be used:\|[0068] Starting with a magnesium silicate rock of composition m(MgO).t(QO).SiO2.xH2O, and recycling substantially all of the alkali metal (R) compounds used back into the process, at least two separate major product streams can be secured from amongst the following:\| - (i) Products rich in magnesium oxide or hydroxide (MgO or Mg(OH)2)\| - (ii) Products rich in amorphous silica (SiO2)\| - (iii) Products rich in amorphous magnesium silicate hydrates (M-S—H)\| - (iv) Products rich in magnesium carbonate compounds, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3, also known as magnesite); or magnesium carbonate trihydrate (MgCO3.3H2O, also known as nesquehonite); or magnesium hydroxy-carbonate hydrate, such as\|[0073] (Mg(OH)2.4MgCO3.4H2O), also known as hydromagnesite, or (Mg(OH)2.MgCO3.3H2O), also known as artinite.\|[0074] Improved separation of the above major solid product streams can also be achieved by the application of other known mineral separation techniques such as, for example, flotation. Such flotation techniques can be effected using flotation aids including sodium oleate, carboxymethylcellulose and methyl isobutyl carbinol.\|[0075] To the extent that CO2 is produced by the combustion of fuels used in the process, e.g. to heat the kiln or furnace, or to dry materials, this CO2 can be captured in the process in the form of product (iv) listed above, by using a treatment process based on the reactions shown above. To the extent that the process is energy-efficient, the aforesaid CO2 produced by the combustion of fuels used in the process, even if substantially completely captured by reactions of the sort shown, for example, in equations (3), (4) and (5), will generally not be sufficient to convert all of the magnesium in the process to product stream (iv), leaving some of the magnesium available for the production of product streams (i) and (iii). However, in another embodiment of the process, additional CO2 can be obtained from other sources and included in the treatment process and thus captured. In such a case, it is possible to operate the process in such a way that product stream (i) is not produced, but the process itself becomes a net consumer of CO2. Moreover, it is also possible to operate the process without separating any of the product streams, so that the only product stream produced is a mixture of some or all of the above product streams\|[0076] In a further approach, the process uses the same magnesium silicate raw material as shown above, but in this case, not all of the alkali metal-rich products of the process are recycled within the process. It is therefore possible to have one or more additional product streams as well as those already listed above. For example, one very useful product stream is an alkali metal silicate, (R2SiO3), either in the form of an alkaline aqueous solution also containing alkali metal hydroxides and/or carbonates, or as a solid product, (for example, obtained by evaporation and/or crystallization).\|[0077] According to a feature of the invention the process further comprises carbonation of the second composition, e.g. by treatment with gases containing CO2, to produce a third composition comprising a magnesium carbonate, e.g. either simple magnesium carbonates, such as anhydrous magnesium carbonate itself (MgCO3), also known as magnesite; or magnesium carbonate trihydrate (MgCO3.3H2O), also known as nesquehonite; or magnesium hydroxy-carbonate hydrates, such as (Mg(OH)2.4MgCO3.4H2O), also known as hydromagnesite, or (Mg(OH)2.MgCO3.3H2O), also known as artinite.\|[0078] According to a further feature of the invention, the process further comprises conducting the carbonation of the second composition as described in the preceding paragraph, but where the second composition is first formed by moulding or pressing to form a shaped article, such that the resulting final carbonated composition retains the form of the shaped article but is further hardened by the formation of magnesium carbonates in situ. The present invention thus provides a process as described hereinbefore, in which the carbonation of the second composition is conducted in a second step, after a first step during which the second composition is formed by moulding or pressing to form a shaped article, such that a carbonated shaped article is obtained.\|[0079] The present invention further provides a carbonated shaped article obtained by the process as described hereinbefore.\|[0080] According to a further feature of the invention the process further comprises calcining the magnesium carbonate from the third composition to produce a fourth composition comprising magnesium oxide.\|[0081] The invention also provides a process in which a product comprising a transition metal such as iron, nickel and/or chromium compound is produced.\|[0082] Another useful product stream is rich in transition metal oxides, for example iron oxides such as magnetite (Fe3O4), and which may also contain significant amounts of chromium and/or nickel oxides. These oxides can be concentrated by flotation and/or magnetic separation.\|[0083] Another useful product stream is an alkaline solution containing chromates, which can be treated with a reducing agent and pH control (or by electrochemical reduction) to separate relatively pure chromium oxides, or even chromium metal; for example:\|R2CrO4(aqueous solution)+(reducing agent)Cr(OH)3(solid precipitate)\|[0084] In this specification, including the accompanying claims, percentages unless otherwise indicated are by mass.\|[0085] The term “pellets” as used in this specification including the accompanying claims is to be understood as embracing shaped, generally substantially spherical, forms such as pellets, nodules and granules.\|[0086] Particle size distribution when measured by laser granulometry is measured using a Malvern MS2000 laser granulometer. Measurement is effected in ethanol. The light source consists of a red He—Ne laser (632 nm) and a blue diode (466 nm). The optical model is that of Mie and the calculation matrix is of the polydisperse type.\|[0087] The apparatus is checked before each working session by means of a standard sample (Sifraco 010 silica) for which the particle size distribution is known.\|[0088] Measurements are performed with the following parameters: pump speed 2300 rpm and stirrer speed 800 rpm. The sample is introduced in order to establish an obscuration between 10 and 20%. Measurement is effected after stabilisation of the obscuration. Ultrasound at 80% is first applied for 1 minute to ensure the de-agglomeration of the sample. After about 30 s (for possible air bubbles to clear), a measurement is carried out for 15 s (15000 analysed images). Without emptying the cell, measurement is repeated at least twice to verify the stability of the result and elimination of possible bubbles.\|[0089] All values given in the description and the specified ranges correspond to average values obtained with ultrasound.\|[0090] It is to be understood that in the foregoing text, unless otherwise specified, the symbols R, Q, m, t, x and, p are as initially defined.\|[0091] The following non-limiting Examples illustrate embodiments of the invention.\|[0092] The following abbreviations and notations are used:\| - XRF X-ray fluorescence\| - XRD X-ray diffraction\| - ICP Inductively-Coupled Plasma Photometry\| - Hydromagnesite Mg(OH)2.4MgCO3.4H2O\| - Artinite Mg(OH)2.MgCO3.3H2O\| - Eitelite Na2CO3.Mg(CO3)\| - LOI Loss on ignition\|(US9631257)\|EXAMPLE 1\|[0100] Ground pure olivine sand (Mg0.94Fe0.06)2SiO4 was mixed with sodium carbonate hydrate powder in a 14:11 mass ratio. The molar ratio of this mixture is close to 1:1. 25 g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. It was heated up to 800° C. over 2 hours, maintained at 800° C. for 1 hour and cooled back to room temperature by natural cooling. In order to evaluate the reaction efficiency, separate samples of the sodium carbonate and olivine used underwent exactly the same heat treatment. The measured ignition losses are shown in the following Table.\|[0101] SampleLoss on Ignition Sodium carbonate powder14.97% Ground olivine sand0.22% 14:11 mix of ground olivine sand +16.69% sodium carbonate powder \|[0102] The ignition loss of the pure sodium carbonate was due entirely to loss of hydrate water and not to decomposition or evaporation of the carbonate. The pure olivine sample remained essentially unchanged during heat treatment, but the mixed sample reacted. From the measured LOI data, it is estimated that 60% of the CO2 from the carbonate was lost from the mixture. The phase constitution of the reacted sample was determined by XRD. The reaction products observed by this technique were Na2MgSiO4, MgO and Fe2O3 together with some unreacted olivine and sodium carbonate.\|[0103] 10 g of the reacted sample was put into 100 ml of de-ionised water under constant stirring at 40° C. for 1 h in order to evaluate its dissolution behaviour. The solution was filtered and the solid residue was analysed by XRD. The amounts of dissolved elements in the aqueous solutions were measured by ICP.\|[0104] The main solid phases detected in the filtered solid residue were Na2MgSiO4, MgO, Fe2O3 and olivine. All non-reacted sodium carbonate dissolved in the aqueous solution. Additionally, some dissolved SiO2 was detected with a concentration of 667 mg/I. From this value, one can estimate that 2 to 3% of the total silica from the mixture dissolved in the water under these conditions, (presumed to be as a sodium silicate, as the pH of the solution was measured to be about 12).\|EXAMPLE 2\|[0105] The same ground pure olivine sand (Mg0.94Fe0.06)2SiO4 and sodium carbonate hydrate powder as used in Example 1 were mixed in a 1400:1235 mass ratio. The molar ratio of this mixture is approximately 1:1. The powder was pressed into pellets and placed (in a platinum crucible) into a lab furnace which was kept at 900° C. The sample was air-quenched after 1 h of heat treatment. Separate samples of the sodium carbonate and olivine used underwent an identical heat treatment. It is important to mention that at this temperature, sodium carbonate is in the liquid state. (The melting temperature of this compound is 851° C.). The measured loss on ignition of all of the samples is presented in the following Table.\|[0106] SampleLoss on Ignition Sodium carbonate14.96% Olivine0.04% Olivine + Sodium carbonate23.02% \|[0107] From the measured LOI data, a conversion rate (degree of decarbonation) close to 100% was obtained which means that the reaction was essentially complete. The reaction product was analysed by XRD and the phases detected were Na2MgSiO4, MgO, NaFeO2 together with some un-reacted olivine. No remaining sodium carbonate was detected, in agreement with the observed loss on ignition data. The MgO to Na2MgSiO4 mass ratio was estimated by Rietveld analysis of the XRD data to be 14:86, in reasonable agreement with mass balance calculations.\|EXAMPLE 3\|[0108] 13 g of the powdered product of Example 2 was mixed with 260 ml of water to give a slurry with about 50 g/L solids concentration. This slurry was put in a closed pressure reactor with a total volume of 2 liters, maintained at 25° C. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas and the pH of the aqueous solution were recorded as functions of time and are presented in FIG. 2. The rate of pressure drop indicates that the slurry captures gaseous CO2 rapidly, and, concurrently, the pH of the solution falls rapidly from an initial value of over 12 to a final value of about 8.5, consistent with the formation of a mixed sodium carbonate/bicarbonate solution. After this reaction the solids in the slurry were filtered and analysed by XRD. NaFeO2 was no longer detectable and the MgO:Na2MgSiO4 ratio had increased to an estimated value of 18:82, indicating that some sodium silicate had leached out of the Na2MgSiO4 phase into the solution and had then been carbonated.\|EXAMPLE 4\|[0109] 5 g of the powdered product of Example 2 was mixed with 200 ml of water to give a slurry of about 25 g/L solids concentration. This slurry was then boiled gently for one hour, after which it was filtered and the solid residue analyzed by XRD. The relative concentration of the Na2MgSiO4 phase in the residue was clearly greatly reduced compared to the original untreated residue, and the relative concentration of MgO greatly increased. The NaFeO2 phase had also completely disappeared but peaks for a layered double hydroxide phase probably having a formula close to 4MgO.Fe2O3.CO2.10H2O were seen clearly, together with weaker peaks for Fe2O3 (haematite) and unreacted olivine.\|[0110] The liquid filtrate was also analyzed by ICP and the results (see the Table below) showed a high concentration (6.92 g/L as Na2O) of sodium in solution, as well as 0.47 g/L of SiO2. This confirms that most of the sodium had leached out of the sample, and that about 15% of it was probably in the form of a sodium metasilicate solution, the rest presumed to be a mixture of sodium hydroxide and sodium carbonate.\|[0111] Chemical analysis of the aqueous solution Chemical speciesConcentration [mg/l] SiO2466 Al2O36.65 Fe2O31.78 CaO0.51 MgO1.51 K2O2.40 Na2O6920 SO32.53 P0.58 \|EXAMPLE 5\|[0112] The powdered product of Example 2 was mixed with water to give slurries (suspensions) with various solids concentrations, in some cases with the addition of various soluble salts to the initial aqueous solution. A sample of slurry was put in a closed reactor with a total volume of 1.65 liters, maintained at 35° C. and agitated with a mechanical stirrer operating at 500 rpm. The reactor was first evacuated and then filled with pure gaseous CO2 up to one atmosphere pressure. The pressure of the gas, which decreased with time due to its absorption by the slurry, was recorded continuously. Whenever the pressure reached a relatively constant value, further CO2 was added again to bring it back to one atmosphere. By following the change of pressure with time between refills, it was possible to estimate the total amount of CO2 consumed by reaction with the slurry. Results for a series of such experiments are summarized in the following Table.\|[0113] CO2 Total captured, CO2Slurry SlurryTotalas % of Experimentcapturedvolumeconc.solids. theoreticalSlurryTemp.DurationSolid productsn° (mol)(mL)(g/L)(g)maximumadditives(° C.)(h)detected 10.06412605013.035Na2CO3:3524Hydromagne 21.15 g/L site20.07242605013.040Na2CO3:3524Hydromagne 53.85 g/L site30.13632605013.075NaHCO3:3530Hydromagne 53.85 g/L site40.035226011.52.9984 3526Artinite \|[0114] The theoretical maximum CO2 capture was calculated on the assumption that all of the carbonatable solids, expressed in terms of MgO and Na2O in the solids, would carbonate to give MgCO3 and Na2CO3, respectively, irrespective of any slurry additives present. However, it was observed that the main solid products were usually hydromagnesite and, in one case, artinite, which would imply a slightly lower amount of CO2 capture than the maximum theoretical value. In experiment 4, during which no slurry additives were used (i.e. pure water was used to make the slurry) the amount of CO2 captured, at 84% of theoretical, is actually slightly more than would be expected if artinite were the main magnesium carbonate formed, so it is likely that other carbonates were also formed but not detected. In any case, the result of experiment 4 shows that it is possible to essentially fully carbonate an aqueous suspension of the reaction product of Example 2 in about one day at atmospheric pressure. (Note also that the duration of these experiments was probably longer than necessary because they had to be left overnight unattended, during which time no additional CO2 could be added to bring the pressure back up. If one atmosphere pressure of CO2 had been maintained continuously, the reaction times would probably have been significantly shorter).\|EXAMPLE 6\|[0115] A crushed sample of serpentine from Horsmanaho, Finland (ground in a ball mill to a powder with 43% passing a 75 micrometer sieve, and containing, by mass, 37.9% silicon expressed as SiO2, 38.7% magnesium expressed as MgO, 7.4% iron expressed as Fe2O3, and with an ignition loss of 14.9% at 950° C.), was mixed with anhydrous sodium carbonate powder in a 5355:4645 mass ratio (molar ratio approximately 1:1.3). About 5 kg of the mixed powder was pressed into a steel crucible and calcined in a lab furnace at 950° C. for 4.5 hours. The mass loss during calcination was 27.9%. From the measured mass loss it can be estimated that the decarbonation reaction was complete. The reaction product was analysed by XRF spectrometry and shown to contain 27.8% silicon expressed as SiO2, 30.4% magnesium expressed as MgO, 5.7% iron expressed as Fe2O3, and 33.4% sodium expressed as Na2O. An XRD analysis showed the major phases present in the product to be Na2MgSiO4 and periclase (MgO).\|EXAMPLE 7\|[0116] The reaction products of Example 2 (referred to hereinafter as “product X”) and of Example 6 (referred to hereinafter as “product XS”) were ground to powders, and the finenesses of the resulting powders were measured using the Blaine Specific Surface Area (BSS) method. For each sample of product X or XS, 75 g of the solid were added to 1.5 liters of deionized water in a glass reactor equipped with a stirrer with a helicoidal Teflon® paddle operating at 500 rpm. Pure CO2 gas was bubbled continuously through the agitated suspension (via a porous glass frit at the bottom) at a flow rate of 12 normal liters per hour at close to one atmosphere absolute pressure. The reactor contents were maintained at 70° C. by a jacket heated by circulating hot water. After various periods of time, samples of the suspension were taken to assess the progress of the carbonation reaction. The samples were filtered and the liquid filtrates were analysed for dissolved elements by ICP. The solid filter-cakes were dried at 110° C. and then analysed by XRF spectrometry for elemental composition, by XRD for qualitative phase composition, and by thermal analysis coupled with evolved gas analysis for the quantitative detection of combined CO2 and water. In order to calculate the amount of magnesium that had reacted, it was assumed that all of the CO2 in the dried filter-cake was present in the form of hydromagnesite.\|[0117] The results for three different product samples are given in the following Table\|[0118] Blaine EstimatedMg inEstimated specificMainTotal Mg Mg inaqueousdegree of surfacecrystallinecontent ofCO2hydro-phasereaction ofExperiment area ofphasesdried filter-contentmagnesiteexpressedMgO inN°; anhydrousdetected incake,of driedexpressedas % MgOanhydrousanhydrousDurationproduct,dried filter- expressedfilter-as % MgOrelative toproduct,product used(h)m2/kgcakeas MgO, %cake, %in filter-cakefilter-cake% 53.5420Hydro-31.215.918.20.659Product X magnesite 614.0600Hydro-30.316.418.80.563Product X magnesite 74.0205Hydro-27.717.219.70.471Product magnesite XS 1In experiment 6, a high-power agitation system was used instead of the normal stirrer\|[0119] It can be seen from the above results that it is possible to carbonate products X and XS at only one atmosphere pressure in aqueous suspension and obtain conversion yields of the order of 60-70% of the total magnesium in the starting material in about 3.5 to 4 hours. Based on XRF analyses of the solid phases coupled with ICP analyses of the liquid phase, it is estimated that roughly 90% of the initial Na and 50% of the initial Cr in the product leached out during the experiment.\|EXAMPLE 8\|Formation of Eitelite\|[0120] The procedure of Example 7 was repeated using two slurries (prepared from products X and XS from Examples 2 and 6, respectively) at a concentration of 150 g/L, i.e. three times the concentration used in Example 7.\|[0121] During the 3 first hours the same trends were observed as those in Example 7. But after 4 hours, XRD revealed the presence of eitelite as well as hydromagnesite. The results are given in the following Table.\|[0122] Blaine Mg inEstimated specificMainTotal Mg Estimatedaqueousdegree of surface areacrystallinecontent ofCO2Mg in hydro-phasereaction ofExperiment ofphasesdried filter-contentmagnesiteexpressedMgO inN°; anhydrousdetectedcake,of driedexpressedas % MgOanhydrousanhydrousDurationproduct,in driedexpressedfilter-as % MgO inrelative toproduct,product used(h)m2/kgfilter-cake as MgO, %cake, %filter-cakefilter-cake% 84.0600Hydro-28.0616.4518.830.567.12Product X magnesite & eitelite 94.0600Hydro-25.7415.8218.110.870.37Product magnesite XS & eitelite \|EXAMPLE 9\|Effectiveness of Water Leaching\|[0123] 50 g of product X was washed in 1 L deionised water 6 times in series (15 minutes stirring in between at room temperature and atmospheric pressure, i.e. 25° C. and 1 bar). Each time a small sample was taken to analyse the solids and the liquids. The XRF results for product X coupled with ICP solution analyses lead to the results given in the following Table, which the percentages of each element leached from the product are given as a function of the number of washing steps.\|[0124] % leachedSiCaMgKNaSCr Washing 19.850.460.0019.7636.4413.7746.12Washing 23.200.090.00 1.94 8.69 0.60 1.30Washing 31.410.020.00 0.25 3.47 0.04 0.21Washing 41.220.020.00 0.03 3.53 0.13 0.32Washing 50.750.020.00 0.02 1.87 0.14 0.12Washing 60.510.050.00 0.00 1.30 0.05 0.08TOTAL16.940.660.0122.0055.3114.7348.15 \|[0125] The first washing step was clearly the most efficient. Therefore 500 g of product X were washed in the same conditions, the solid was then filtered and dried overnight at 110° C. Finally the same carbonation experiment as described in Example 8 was performed on this solid product. This time XRD analysis revealed only hydromagnesite; no eitelite was detected. This shows that washing can be used to enhance Na recycling in the process.\|[0126] The analysis of the solution obtained after the first washing (table below) showed it to have a high pH and to contain about 4000 mg/L of Na and 637 mg/L of Si, the other elements being present in much smaller amounts. On this basis, the solution was estimated to contain about 23 milimoles/liter of sodium metasilicate (Na2SiO3) and 130 millimoles/liter of sodium hydroxide (NaOH), possibly also including some carbonate ions.\|[0127] In mg/l (elements)SiCaMgKNaSCr Washing 1637.50.2990.2674.140001.3828.4 \|EXAMPLE 10\|Hydromagnesite Formation at 60° C.\|[0128] 1 L of a 50 g/L slurry of product X was prepared and poured into a 2 L autoclave. The system was closed and 1 L of pure CO2 at 10 bars was added without purging the residual air, after which the slurry was stirred and heated up to 60° C. (which roughly corresponds to the dew point of exhaust gases in a cement plant). After 2 hours the pressure dropped to close to atmospheric and heating of the autoclave was stopped. The next day, the slurry was filtered and dried overnight at 110° C. XRD revealed hydromagnesite as the main crystalline product.\|EXAMPLE 11\|Formation of Magnesite as Main Product at 120° C.\|[0129] The procedure of Example 10 was repeated but at 120° C. (a typical temperature for exhaust gases from a cement plant) using the same autoclave, and adding CO2 each time the pressure dropped close to two bars (the equilibrium water vapour pressure at 120° C.). Three additions of CO2 up to 10 bars were made in the space of one day. XRD on the dried solid revealed magnesite (MgCO3) to be the main product, but also showed some traces of magnetite (Fe3O4). ICP analysis of the aqueous phase showed 90% leaching of Na. The combined CO2 content in the solids was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser and showed that the amount of MgCO3 present accounted for about 47% of the original Mg in Product X.\|EXAMPLE 12\|Selective Separation of Chromium by Reduction in Solution\|[0130] Powdered product X was stirred with deionised water for 15 minutes at a 2:1 Water:solids mass ratio. The yellow-coloured aqueous phase was filtered and a sample taken for ICP analysis. Excess ferrous sulfate (FeSO4), a reducing agent, was then added in powder form to the solution, after which a chromium-containing precipitate formed. The liquid was again filtered, giving a colourless solution which was again analysed by ICP. The chromium content of the yellow-coloured aqueous phase was 772 mg/L. The colourless solution contained only 29 mg/L of chromium.\|[0131] These results, when compared with the analysis of the raw materials, indicated that about 50% of the total chromium in the original raw material (olivine) was converted into a readily soluble (chromate) form by the process used to make “product X,” and 96% of the Cr leached into the solution was precipitated by addition of ferrous sulfate.\|EXAMPLE 13\|Concentration of Hydromagnesite from the Solid Residues by Flotation\|[0132] Separation tests were performed by flotation on the carbonated products produced from the application of the process to olivine and serpentine, similarly to the products shown, respectively, for experiments 5 and 7 in the table of Example 7. Combinations of sodium oleate, carboxymethylcellulose (CMC) and methyl isobutyl carbinol (MIBC) were used in the aqueous phase sequentially to disperse the solids in the form of a slurry at a solids concentration of 90 g/L.\|[0133] First sodium oleate was added to the slurry and stirred for 5 minutes in a beaker in order to render carbonated particles hydrophobic. Then CMC was added to depress silicate hydrophobicity, followed by a further 5 minutes of stirring; and finally MIBC was added in order to stabilise the foam formed by air bubbling.\|[0134] Air was bubbled through the treated slurry in a miniature flotation cell, and the solids carried over by the foam were collected as “concentrate.” The residual solids were collected as “tailings.” Results of four such experiments are presented in the table below. The CO2 content was analysed by means of a high-frequency induction furnace coupled to a Horiba EMIA-820V gas analyser. The CO2 contents of the concentrates were typically 3-4 times greater than those of the tailings, showing that hydromagnesite can be effectively separated by flotation in this manner.\|[0135] The XRD results confirm the separation. They are expressed in a qualitative way by different symbols expressing the probability of a phase presence:\| - (o) not present,\| - () possibly present,\| - (X) definitely present,\| - (X+) present in abundance.\|[0140] Chemical additive (dosage, ppm)Test 1Test 2Test 3Test 4 Sodium oleate1500100020001000CMC200200200200MIBC20202020Product tested by flotation:Carbonated “product X”Carbonated “product X”Carbonated “product X”Carbonated “product XS”Results of flotation testsTailingsConcentrateTailingsConcentrateTailingsConcentrateTailingsConcentrateComponents SiO2 %34.117.633.718.533.822.033.316.9measured byFe2O3 %6.43.46.43.66.44.36.93.0chemical MgO %34.637.234.537.233.936.929.235.9analysisNa2O %2.31.32.31.42.61.32.31.2 LOI %22.340.022.638.922.735.126.241.6 CO2 %5.722.25.820.25.717.39.423.0Phases Sodium 00000000detected bymagnesium XRDsilicate PericlaseXXX** OlivineXXX*00 HydromagnesiteXX +XX +XX +XX + \|EXAMPLE 14\|[0141] Ground natural talc from Luzenac (France) with nominal composition Mg3Si4O10(OH)2 and containing some minor impurities (1.1% Al2O3, 0.9% Fe2O3 and 0.9% CaO by mass) was mixed with anhydrous sodium carbonate (Na2CO3) at a 4863:5136 mass ratio (molar ratio approximately 1:1). The composition was chosen in order to obtain an atomic ratio of 2:1 Na:Si in the final sample. 20.5 g of this powder was pressed into a pellet and placed into a lab furnace in a platinum crucible. The sample was heated at 900° C. for 1 hour, followed by cooling in air. It was weighed before and after treatment and the measured loss on ignition of 23.3% was consistent with evaporation of carbon dioxide from the sodium carbonate plus bound water from the talc; it represents about 95% of the theoretical value for complete reaction of 24.6%. The phase constitution of the reacted sample was determined by X-ray diffraction: the main products detected were Na2MgSiO4 and Na2SiO3.\|EXAMPLE 15\|[0142] A sample of Product X was leached in water following a procedure similar to that given in example 9. After drying at 105° C., the powdered material (which had an ignition loss of 8.9%), was analyzed by X-ray fluorescence for its major elements, and found to contain 28.1% SiO2, 39.1% MgO and 17.9% Na2O. An X-ray diffraction analysis showed that the main crystalline compounds present in the powder were periclase (MgO), sodium magnesium orthosilicate (Na2MgSiO4) and forsterite olivine (Mg2SiO4); but it was known also to contain amorphous magnesium silicate hydrates (M-S—H). 5 parts of this material were mixed manually with 1 part of deionised water in a rubber bowl, using spatula. 7 g aliquots of the resulting paste were compressed in a cylindrical mould at a load of 3 tonnes to give cylindrical pellets 19 mm in diameter and 10 mm in height. These pellets were subject to curing in a flow of pure CO2 gas at atmospheric pressure in a chamber at 20±2° C. Two different humidity conditions were tested: dry (i.e. no water added to the gas stream); and wet (in which the gas stream was bubbled through water at the bottom of the curing chamber before passing over the pellets). The uptake of CO2 and/or water by the pellets was followed by taking them out quickly and weighing them once a day. The experiment was stopped after one week, as the weight increases had begun to level off. At this point, the pellets carbonated under dry conditions had gained 3.0% and all four of the pellets tested gave essentially identical weight changes. On the other hand, the pellets carbonated under wet conditions (close to 100% relative humidity) showed a wider pellet-to pellet variation in weight increase, with a mean of 7.8% and a standard deviation of about 1%.\|[0143] It was notable that all of the pellets that had been carbonated under one atmosphere of CO2 became superficially much harder than companion pellets that had simply been stored in air. The pellets carbonated under humid conditions also showed a considerable amount of efflorescence. A sample of this efflorescence was scraped off and analyzed by X-ray diffraction. It was found to contain nesquehonite (MgCO3.3H2O), nahcolite (NaHCO3), trona (Na3H(CO3)2.2H2O), and sodium carbonate mono-hydrate (Na2CO3.H2O). The wet-carbonated pellets themselves, analyzed by the same technique, showed the presence of primarily of periclase (MgO), sodium magnesium orthosilicate (Na2MgSiO4), olivine (Mg2SiO4) and nesquehonite (MgCO3.3H2O). It thus appears that nesquehonite was the main “binder” phase and that it was probably produced to a significant extent by carbonation of M-S—H.\|[0144] Pairs of treated and untreated pellets were compressed to failure in a compression machine. The results are summarized in the table below:\|[0145] Compressive loads at failure,Curing regime applied to pressed pelletskN, (for 2 pellets) Stored in air3.0; 3.2Carbonated under humid conditions11.5; 18.5Carbonated under dry conditions36.0; 36.7 \|[0146] It is clear that the atmospheric-pressure carbonation process greatly increased the strength of the pellets, and that carbonation under dry conditions was preferable to carbonation under humid conditions.	Family Number\|(66131709)\|66131709\|Advantages / Prev. Drawbacks\|(WO201482996 A1)\|According to one manufacturer of such products hectorites have the formula (Mg5.2Lio.8)(Si8)02o(OH)4Nao.8- The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (C02) and which can be subjected to further treatments to produce a number of useful products.\|(CA2892325 A1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO 2 ) and which can be subjected to further treatments to produce a number of useful products.\|(AU2013351282 B2)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|(AU2013351282 A1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|(CN104812468B B)\|The present invention seeks to provide a process for producing alkali metal magnesium orthosilicates and magnesium oxide and / or alkali metal silicates from magnesium silicate rocks and which can be used to undergo chemical action to capture carbon dioxide ( CO ) 2 ) And may be subjected to further processing to produce a variety of useful products . \|(CN104812468 A)\|The present invention seeks to provide a process for producing alkali metal magnesium orthosilicates and magnesium oxide and / or alkali metal silicates from magnesium silicate rocks and which can be used to undergo chemical action to capture carbon dioxide ( CO ) 2 ) And may be subjected to further processing to produce a variety of useful products . \|(KR20150088845 A)\|The present invention relates to carbon dioxide (Co2alkali metal magnesium orthosilicate and magnesium oxide and/or alkali metal silicate from magnesium silicate rock, which can be used in chemical treatments that capture a number of useful products and can be subjected to further treatments to produce a number of useful products.\|(US9631257 B2)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|(US20150299823 A1)\|The present invention seeks to provide a process for the production from magnesium silicate rock of alkali metal magnesium orthosilicates and magnesium oxide and/or alkali metal silicates which can be used subjected to chemical to capture carbon dioxide (CO2) and which can be subjected to further treatments to produce a number of useful products.\|	Chemical engineering\|Environmental technology\|Materials, metallurgy	B01D-053/62\|B01D-2251/402\|B01D-2253/106\|B01D-2257/504\|B01J-020/10\|B01J-020/30/85\|C01B-033/22\|C01B-033/24\|C01B-033/32\|C01F-005/06\|C01F-005/24\|C04B-028/10\|C04B-028/18\|C04B-028/18/4\|C04B-2111/00019\|C22B-001/00\|C22B-026/22\|Y02C-010/04\|Y02C-020/40\|Y02P-010/146\|Y02P-020/151\|Y02P-020/152\|Y02P-040/18	(GR1) C04B-028/18/4[RK1]; 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Лидин Р.А., Москва, Дрофа, 2007, с. 285.	US3954943; WO2009132692; WO200769902; WO201097451; XP002994928; US20040213705; EP2532624\|US3954943; RU2011111500; WO2009132692\|US3954943; WO2009132692; EP2532624; US4478796; US20080112868; US20100151243; US20120291675; US2008112868; US2010151243; US2012291675\|US4478796; US20080112868; CN101607721\|US4478796; US20080112868; US20100151243; US3954943; US5085838; US6054106; US20040213705; US20120291675; EP2508496; EP2532624; WO200769902; WO2009132692; WO2009156740; WO201097451; XP002994928\|JP11512376; US3954943; JP2009084132\|US3954943; WO2009132692; WO200769902; WO201097451; US20040213705; EP2532624; US-837672; US20120291675\|\|\|	(EP2925426)\|Examiner references\|-See also references of WO 2014082996A1\|\|(US9631257)\|Applicant references\|-International Search Report as issued in International Patent Application No. PCT/EP2013/074732, dated Mar. 11, 2014.\|-O'CONNOR W K, ET AL.: "Carbon dioxide sequestration by direct mineral carbonation: process mineralogy of feed and products.", MINERALS AND METALLURGICAL PROCESSING., SOCIETY FOR MINING, METALLURGY AND EXPLORATION, US, vol. 19, no. 2, 1 May 2002 (2002-05-01), US, pages 95 - 101, XP002994928, ISSN: 0747-9182\|\|(WO2014/082996)\|International Search Report [Examiner]\|-O'CONNOR W K ET AL: "Carbon dioxide sequestration by direct mineral carbonation: process mineralogy of feed and products", MINERALS AND METALLURGICAL PROCESSING, CO, vol. 19, no. 2, 1 May 2002 (2002-05-01), pages 95 - 101, XP002994928, ISSN: 0747-9182\|-See also references of EP 2925426A1\|\|\|\|\|\|\|\|	PENDING	(EP2925426)\|LAPSED\|(US9631257)\|LAPSED\|(WO2014/082996)\|LAPSED\|(JP2015536897)\|REVOKED\|(CN104812468)\|LAPSED\|(RU2654983)\|LAPSED\|(AU2013351282)\|EXPIRED\|(MX2015006607)\|PENDING\|(KR10-2015-0088845)\|LAPSED\|(CA2892325)\|LAPSED	ALIVE	(EP2925426)\|DEAD\|(US9631257)\|DEAD\|(WO2014/082996)\|DEAD\|(JP2015536897)\|DEAD\|(CN104812468)\|DEAD\|(RU2654983)\|DEAD\|(AU2013351282)\|DEAD\|(MX2015006607)\|ALIVE\|(KR10-2015-0088845)\|DEAD\|(CA2892325)\|DEAD	(EP2925426)\|LEGAL DETAILS FOR EP2925426\|Actual or expected expiration date=2018-04-10\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=EP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=EP EP13795508\|Application date=2013-11-26\|Standardized application number=2013EP-0795508\|Event publication date=2015-09-04\|Event code=EP/PUAI\|Event group=Administrative notifications\|PUBLIC REFERENCE MADE UNDER ARTICLE 153(3) EPC TO A PUBLISHED INTERNATIONAL APPLICATION THAT HAS ENTERED THE EUROPEAN PHASE\|Publication in section i.1 EP bulletin\|Original code: 0009012\|Event publication date=2015-10-07\|Event code=EP/A1\|Event group=Examination events\|Application published with search report\|Publication country=EP\|Publication number=EP2925426\|Publication stage code=A1\|Publication date=2015-10-07\|Standardized publication number=EP2925426\|Event publication date=2015-10-07\|Event code=EP/17P\|Event indicator=Pos\|Event group=Examination events\|Request for examination filed\|Pruefungsantrag gestellt\|Effective date of the event=2015-06-29\|Event publication date=2015-10-07\|Event code=EP/AK\|Event indicator=Pos\|Event group=Designated states\|Designated contracting states:\|Benannte vertragsstaaten\|Designated contracting states=AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR\|Event publication date=2015-10-07\|Event code=EP/AX\|Event indicator=Pos\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT\|Request for extension of the european patent to\|Designated contracting states=BA ME\|Event publication date=2015-12-09\|Event code=EP/RAP1\|Event group=Change of name or address Reassignment\|Rights of an application transferred\|Anmelder uebertragung (korr.)\|OWNER:LAFARGE\|Event publication date=2016-03-02\|Event code=EP/DAX\|Event group=Designated states\|REQUEST FOR EXTENSION OF THE EUROPEAN PATENT (DELETED)\|Request for extension of the european patent (to any country) deleted\|Event publication date=2016-06-15\|Event code=EP/17Q\|Event indicator=Pos\|Event group=Examination events\|First examination report\|Erster pruefungsbescheid\|Effective date of the event=2016-05-13\|Event publication date=2018-08-10\|Event code=EP/STAAABN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The application is deemed to be withdrawn\|Original code: STAA\|Event publication date=2018-09-12\|Event code=EP/18D\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Application deemed to be withdrawn\|Effective date of the event=2018-04-10\|(US9631257)\|LEGAL DETAILS FOR US9631257\|Actual or expected expiration date=2021-05-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=US/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=US US14647277\|Application date=2013-11-26\|Standardized application number=2013US-14647277\|Event publication date=2013-11-26\|Event code=US/EXMR\|Event group=Administrative notifications\|USPTO Examiner Name\|PRIMARY EXAMINER:SOLIMAN, HAYTHAM\|Event publication date=2013-11-26\|Event code=US/ART\|Event group=Administrative notifications\|USPTO Art Group\|ART=1736\|Event publication date=2013-11-26\|Event code=US/DK\|Event group=Examination events\|Attorney Docket Number\|Docket Nbr: 035112-0439264\|Event publication date=2013-11-26\|Event code=US/CUST\|Event group=Examination events\|Attorney/Agent Customer Number\|Customer Nbr: 909\|Event publication date=2013-11-26\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Business Entity Status: Regular Undiscounted\|Event publication date=2013-11-26\|Event code=US/AIA\|Event group=Administrative notifications\|First Inventor File Indicated:\|AIA=No\|Event publication date=2015-05-26\|Event code=US/APE\|Event group=Corrections\|Preliminary amendments\|Event publication date=2015-05-26\|Event code=US/PTARDY\|Event indicator=Pos\|Event group=Examination events\|Patent Term Adjustment - Ready for Examination\|Event publication date=2015-05-26\|Event code=US/IDS\|Event group=Examination events OAI\|Information Disclosure Statement Filed\|Event publication date=2015-05-26\|Event code=US/ENT\|Event group=Administrative notifications\|Entity Status Set to Undiscounted\|Event publication date=2015-06-08\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignors:PISCH, ALEXANDER;GARTNER, ELLIS;MEYER, VINCENT;SIGNING DATES FROM 20150518 TO 20150526\|Reel/frame:035803/0664\|OWNER:LAFARGE, FRANCE\|Event publication date=2015-07-13\|Event code=US/APPFILEREC\|Event group=Administrative notifications OAO\|Filing Receipt\|Event publication date=2015-07-13\|Event code=US/M903\|Event indicator=Pos\|Event group=Examination events OAO\|Notice of DO/EO Acceptance Mailed\|Event publication date=2015-08-20\|Event code=US/DOCK\|Event indicator=Pos\|Event group=Examination events\|Case Docketed to Examiner\|Event publication date=2015-09-18\|Event code=US/CTNF\|Event group=Examination events OA OAO\|Non-Final Rejection\|Event publication date=2015-09-23\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2015-09-23\|R4R=102b\|RJST=non-final\|Rejected claims 10\|RJCT=US20100151243\|Event publication date=2015-09-23\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2015-09-23\|R4R=103a\|RJST=non-final\|Rejected claims 1-6; 7\|RJCT=US4478796\|RJCT=US20080112868\|Event publication date=2015-09-24\|Event code=US/102NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 102 - non-novel subject matter in claims\|RJD=2015-09-24\|R4R=102b\|RJST=non-final\|Rejected claims 10\|RJCT=US20100151243\|Event publication date=2015-09-24\|Event code=US/103NF\|Event indicator=Neg\|Event group=Examination events\|Non-final rejection reason 103 - obvious subject matter in claims\|RJD=2015-09-24\|R4R=103a\|RJST=non-final\|Rejected claims 1-6; 7\|RJCT=US4478796\|RJCT=US20080112868\|Event publication date=2015-10-22\|Event code=US/A1\|Event group=Examination events\|Application published\|Publication country=US\|Publication number=US20150299823\|Publication stage code=A1\|Publication date=2015-10-22\|Standardized publication number=US20150299823\|Event publication date=2015-10-22\|Event code=US/PGPUBN\|Event indicator=Pos\|Event group=Examination events OAO\|PG-Pub Issue Notification\|Event publication date=2015-12-28\|Event code=US/CTNFR\|Event group=Examination events OAI\|Response after Non-Final Action\|Event publication date=2016-04-18\|Event code=US/CTFR\|Event group=Examination events OA OAO\|Final Rejection\|Event publication date=2016-04-21\|Event code=US/102FR\|Event indicator=Neg\|Event group=Examination events\|Final rejection reason 102 - non-novel subject matter in claims\|RJD=2016-04-21\|R4R=102b\|RJST=final\|Rejected claims 10\|RJCT=US20100151243\|Event publication date=2016-04-21\|Event code=US/103FR\|Event indicator=Neg\|Event group=Examination events\|Final rejection reason 103 - obvious subject matter in claims\|RJD=2016-04-21\|R4R=103a\|RJST=final\|Rejected claims 1-6; 7\|RJCT=US4478796\|RJCT=US20080112868\|Event publication date=2016-04-22\|Event code=US/102FR\|Event indicator=Neg\|Event group=Examination events\|Final rejection reason 102 - non-novel subject matter in claims\|RJD=2016-04-22\|R4R=102b\|RJST=final\|Rejected claims 10\|RJCT=US20100151243\|Event publication date=2016-04-22\|Event code=US/103FR\|Event indicator=Neg\|Event group=Examination events\|Final rejection reason 103 - obvious subject matter in claims\|RJD=2016-04-22\|R4R=103a\|RJST=final\|Rejected claims 1-6; 7\|RJCT=US4478796\|RJCT=US20080112868\|Event publication date=2016-07-19\|Event code=US/CTFAR\|Event group=Examination events OAI\|Response after Final Action\|Event publication date=2016-08-23\|Event code=US/EXET\|Event group=Examination events OAO INT\|Interview Summary - Examiner Initiated - telephonic\|Event publication date=2016-08-23\|Event code=US/CTAV\|Event group=OAO\|Advisory Action (PTOL-303)\|Event publication date=2016-10-21\|Event code=US/RCEX\|Event group=Examination events RCE OAI\|Request for Continued Examination (RCE)\|Event publication date=2016-10-21\|Event code=US/136G\|Event group=OAO\|Request for Extension of Time - Granted\|Event publication date=2016-10-21\|Event code=US/RCEX\|Event group=Examination events RCE OAI\|Request for Continued Examination (RCE)\|Action Recorded:\|RECD=2016-10-21\|Event publication date=2016-10-24\|Event code=US/DRCECAP\|Event group=RCE OAO\|Disposal for a RCE / CPA / R129\|Event publication date=2016-12-19\|Event code=US/NOAV\|Event group=Examination events OAO\|Notice of Allowance Data Verification Completed\|Event publication date=2016-12-22\|Event code=US/NOAM\|Event indicator=Pos\|Event group=Examination events OAO\|Mail Notice of Allowance\|Event publication date=2017-03-20\|Event code=US/NOARR\|Event group=Examination events\|Response to Reasons for Allowance\|Event publication date=2017-03-20\|Event code=US/N084\|Event group=Payment or non-payment notifications\|Issue Fee Payment Verified\|Event publication date=2017-03-20\|Event code=US/IFEE\|Event group=Payment or non-payment notifications\|Issue Fee Payment Received\|Event publication date=2017-03-21\|Event code=US/APRDY\|Event indicator=Pos\|Event group=Examination events\|Application Is Considered Ready for Issue\|Event publication date=2017-04-05\|Event code=US/ISSM\|Event indicator=Pos\|Event group=Examination events OAO Restitution or restoration\|Issue Notification Mailed\|Event publication date=2017-04-25\|Event code=US/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent as second publication\|Publication country=US\|Publication number=US09631257\|Publication stage code=B2\|Publication date=2017-04-25\|Standardized publication number=US9631257\|Event publication date=2017-04-25\|Event code=US/354\|Event indicator=Pos\|Event group=Extension of term of duration of protection\|Patent term extended under 35 U.S.C 154(b) until/for\|Extension Type=PTA\|Delays (A,B,C): 0 Overlap Delays: 0 Non Overlap Delays: 0\|PTO Office Delays: 0 Applicant Delays: 95 Adjustment total: \|Number of days of extension=0\|Event publication date=2019-01-18\|Event code=US/AS\|Event group=Change of name or address Reassignment\|Assignment\|ASSIGNMENT OF ASSIGNORS INTEREST\|Assignor:LAFARGE\|Reel/frame:048061/0707\|OWNER:HOLCIM TECHNOLOGY LTD, SWITZERLAND\|Effective date of the event=2018-12-10\|Event publication date=2020-05-05\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=3\|Event publication date=2020-12-14\|Event code=US/REM\|Event group=Administrative notifications\|Maintenance Fee Reminder Mailed\|Event publication date=2021-04-25\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Effective date of the event=2021-04-25\|Event publication date=2021-05-31\|Event code=US/FP\|Event indicator=Neg\|Event group=Event indicating Not In Force Payment or non-payment notifications\|Expired due to failure to pay maintenance fee\|Event publication date=2021-05-31\|Event code=US/EXP\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent expired for failure to pay maintenance fees\|Event publication date=2024-05-07\|Event code=US/NMFP\|Event group=Payment or non-payment notifications\|Publication of First Notice of Maintenance Fees Payable.\|Year of payment of annual fees=7\|(WO2014/082996)\|LEGAL DETAILS FOR WO2014/082996\|Actual or expected expiration date=2016-05-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=WO/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=WO WOEP2013/074732\|Application date=2013-11-26\|Standardized application number=2013WO-EP74732\|Event publication date=2014-06-05\|Event code=WO/A1\|Event group=Examination events\|Published application with search report\|Publication country=WO\|Publication number=WO2014/082996\|Publication stage code=A1\|Publication date=2014-06-05\|Standardized publication number=WO201482996\|Event publication date=2016-05-27\|Event code=WO/EETL\|Event group=Event indicating Not In Force\|PCT Application validity period expired.\|MEMBER STATE LEGAL DETAILS FOR AU2013351282\|Actual or expected expiration date=2020-06-25\|Legal state=DEAD\|Status=EXPIRED\|Corresponding cc:\|Designated or member state=AU Corresponding appl: AU2013351282\|Application date in the designated or member state=2013-11-26\|Application number in the designated or member state=2013AU-0351282\|Corresponding cc:\|Designated or member state=AU Corresponding pat: AU2013351282\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2015-06-18\|Publication number in the designated or member state=AU2013351282\|Event publication 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state=CN\|MEMBER STATE LEGAL DETAILS FOR DE\|Actual or expected expiration date=2015-05-27\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=DE\|Event publication date=2015-05-27\|Event code=WO/NENP\|Event group=Event indicating Not In Force\|Non-entry into the national phase\|Corresponding cc:\|Designated or member state=DE\|MEMBER STATE LEGAL DETAILS FOR EP2925426\|Actual or expected expiration date=2018-04-10\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=EP Corresponding appl: EP13795508\|Application date in the designated or member state=2013-11-26\|Application number in the designated or member state=2013EP-0795508\|Corresponding cc:\|Designated or member state=EP Corresponding pat: EP2925426\|Publication stage code in the designated or member state=A1\|Publication date in the designated or member state=2015-10-07\|Publication number in the designated or member state=EP2925426\|Event publication date=2014-07-23\|Event code=WO/121\|Event group=Designated states\|EP: The EPO has been informed by wipo that ep was designated in this application\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2015-05-13\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=EP\|Event publication date=2018-09-12\|Event code=EP/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=EP\|MEMBER STATE LEGAL DETAILS FOR JP2015536897\|Actual or expected expiration date=2018-08-22\|Legal state=DEAD\|Status=REVOKED\|Corresponding cc:\|Designated or member state=JP Corresponding appl: JP2015543468\|Application date in the designated or member state=2013-11-26\|Application number in the designated or member state=2015JP-0543468\|Corresponding cc:\|Designated or member state=JP Corresponding pat: JP2015536897\|Publication stage code in the designated 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in the designated or member state=MX2015006607\|Event publication date=2015-05-26\|Event code=WO/WWE\|Event indicator=Pos\|Event group=Entry into national phase\|Wipo information: entry into national phase\|Corresponding cc:\|Designated or member state=MX\|MEMBER STATE LEGAL DETAILS FOR RU2015125492\|Actual or expected expiration date=2019-11-27\|Legal state=DEAD\|Status=LAPSED\|Corresponding cc:\|Designated or member state=RU Corresponding appl: RU2015125492\|Application date in the designated or member state=2013-11-26\|Application number in the designated or member state=2015RU-0125492\|Corresponding cc:\|Designated or member state=RU Corresponding pat: RU2015125492\|Publication stage code in the designated or member state=A\|Publication date in the designated or member state=2017-01-11\|Publication number in the designated or member state=RU2015125492\|Event publication date=2015-06-29\|Event code=WO/ENP\|Event group=Entry into national phase\|Entry into the national 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cc:\|Designated or member state=US\|Event publication date=2024-05-07\|Event code=US/STCHG\|Patent Status changed by the national office\|Corresponding cc:\|Designated or member state=US\|(JP2015536897)\|LEGAL DETAILS FOR JP2015536897\|Actual or expected expiration date=2018-08-22\|Legal state=DEAD\|Status=REVOKED\|Event publication date=2013-11-26\|Event code=JP/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=JP JP2015543468\|Application date=2013-11-26\|Standardized application number=2015JP-0543468\|Event publication date=2015-09-07\|Event code=JP/A521\|Event group=Examination events\|Written amendment\|Japanese intermediate code: A523\|Effective date of the event=2015-07-23\|Event publication date=2015-12-24\|Event code=JP/A\|Event group=Examination events\|Published application\|Publication country=JP\|Publication number=JP2015536897\|Publication stage code=A\|Publication date=2015-12-24\|Standardized publication 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the Patent Act, Expected Rejection Date\|Effective date of the event=2018-08-22\|(CN104812468)\|LEGAL DETAILS FOR CN104812468\|Actual or expected expiration date=2019-11-26\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=CN/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CN CN201380061823\|Application date=2013-11-26\|Standardized application number=2013CN-80061823\|Event publication date=2015-07-29\|Event code=CN/A\|Event group=Examination events\|Published application\|Publication country=CN\|Publication number=CN104812468\|Publication stage code=A\|Publication date=2015-07-29\|Standardized publication number=CN104812468\|Event publication date=2015-07-29\|Event code=CN/PB01\|Event group=Examination events\|Publication\|Event publication date=2015-11-11\|Event code=CN/SE01\|Event group=Examination events\|Entry into substantive examination\|Event publication date=2017-08-25\|Event code=CN/B\|Event indicator=Pos\|Event group=Event indicating In Force\|Granted patent for invention\|Publication country=CN\|Publication number=CN104812468\|Publication stage code=B\|Publication date=2017-08-25\|Standardized publication number=CN104812468B\|Event publication date=2017-08-25\|Event code=CN/GR01\|Event indicator=Pos\|Event group=Event indicating In Force\|Grant of patent right\|Event publication date=2020-11-06\|Event code=CN/CF01\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Termination of patent right due to non-payment of annual fee\|Effective date of the event=2019-11-26\|(RU2654983)\|LEGAL DETAILS FOR RU2654983\|Actual or expected expiration date=2019-11-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=RU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=RU RU2015125492\|Application date=2013-11-26\|Standardized application number=2015RU-0125492\|Event publication date=2017-01-11\|Event code=RU/A\|Event group=Examination events\|Application for invention\|Publication country=RU\|Publication number=RU2015125492\|Publication stage code=A\|Publication date=2017-01-11\|Standardized publication number=RU2015125492\|Event publication date=2018-05-23\|Event code=RU/C2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent for invention ( 2nd publ.)\|Publication country=RU\|Publication number=RU2654983\|Publication stage code=C2\|Publication date=2018-05-23\|Standardized publication number=RU2654983\|Event publication date=2019-03-01\|Event code=RU/PC41\|Event group=Change of name or address Reassignment\|Official registration of the transfer of exclusive right\|Effective date of the event=2019-03-01\|Event publication date=2019-04-29\|Event code=RU/PC41\|Event group=Change of name or address Reassignment\|Official registration of the transfer of exclusive right\|Effective date of the event=2019-04-29\|Event publication date=2020-09-21\|Event code=RU/MM4A\|Event indicator=Neg\|Event group=Event indicating Not In Force\|The patent is invalid due to non-payment of fees\|Effective date of the event=2019-11-27\|(AU2013351282)\|LEGAL DETAILS FOR AU2013351282\|Actual or expected expiration date=2020-06-25\|Legal state=DEAD\|Status=EXPIRED\|Event publication date=2013-11-26\|Event code=AU/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=AU AU2013351282\|Application date=2013-11-26\|Standardized application number=2013AU-0351282\|Event publication date=2015-06-18\|Event code=AU/A1\|Event indicator=Pos\|Event group=Examination events\|Open to public inspection\|Publication country=AU\|Publication number=AU2013351282\|Publication stage code=A1\|Publication date=2015-06-18\|Standardized publication number=AU2013351282\|Event publication date=2018-03-01\|Event code=AU/B2\|Event indicator=Pos\|Event group=Event indicating In Force\|Patent proceeded by OPI\|Publication country=AU\|Publication number=AU2013351282\|Publication stage code=B2\|Publication date=2018-03-01\|Standardized publication number=AU2013351282\|Event publication date=2018-06-28\|Event code=AU/FGA\|Event indicator=Pos\|Event group=Event indicating In Force\|Letters patent sealed or granted (standard patent)\|Event publication date=2019-02-21\|Event code=AU/PC\|Event group=Change of name or address Reassignment\|Assignment registered\|FORMER OWNER(S): LAFARGE\|OWNER:HOLCIM TECHNOLOGY LTD\|Event publication date=2020-06-25\|Event code=AU/MK14\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Patent ceased section 143(a) (annual fees not paid) or expired\|(MX2015006607)\|LEGAL DETAILS FOR MX2015006607\|Actual or expected expiration date=2033-11-26\|Legal state=ALIVE\|Status=PENDING\|Event publication date=2013-11-26\|Event code=MX/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=MX MX2015006607\|Application date=2013-11-26\|Standardized application number=2015MX-0006607\|Event publication date=2015-08-05\|Event code=MX/A\|Event group=Examination events\|Patent application\|Publication country=MX\|Publication number=MX2015006607\|Publication stage code=A\|Publication date=2015-08-05\|Standardized publication number=MX2015006607\|(KR10-2015-0088845)\|LEGAL DETAILS FOR KR10-2015-0088845\|Actual or expected expiration date=2018-12-27\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=KR/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=KR KR10-2015-7016739\|Application date=2013-11-26\|Standardized application number=2015KR-7016739\|Event publication date=2015-08-03\|Event code=KR/A\|Event group=Examination events\|Published application\|Publication country=KR\|Publication number=KR10-2015-0088845\|Publication stage code=A\|Publication date=2015-08-03\|Standardized publication number=KR20150088845\|Event publication date=2018-12-27\|Event code=KR/WITN\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Withdrawal due to no request for examination\|(CA2892325)\|LEGAL DETAILS FOR CA2892325\|Actual or expected expiration date=2020-08-31\|Legal state=DEAD\|Status=LAPSED\|Event publication date=2013-11-26\|Event code=CA/APP\|Event indicator=Pos\|Event group=Examination events\|Application details\|Application country=CA CA2892325\|Application date=2013-11-26\|Standardized application number=2013CA-2892325\|Event publication date=2014-06-05\|Event code=CA/A1\|Event group=Examination events\|Application laid open\|Publication country=CA\|Publication number=CA2892325\|Publication stage code=A1\|Publication date=2014-06-05\|Standardized publication number=CA2892325\|Event publication date=2018-01-26\|Event code=CA/EEER\|Event indicator=Pos\|Event group=Examination events\|Examination request\|Effective date of the event=2018-01-18\|Event publication date=2020-11-07\|Event code=CA/FZDE\|Event indicator=Neg\|Event group=Event indicating Not In Force\|Dead\|Effective date of the event=2020-08-31	(EP2925426)\|Contracting States: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, LI, RO, NL, TR\|(EP2925426)\|Extension States: ME, BA\|(WO2014/082996)\|ARIPO: GH, RW, GM, LR, TZ, LS, SZ, MW, MZ, SD, UG, NA, ZM, BW, SL, KE, ZW\|(WO2014/082996)\|EAPO: RU, TJ, BY, AZ, TM, AM, KG, KZ\|(WO2014/082996)\|EPO: DE, NO, RS, BE, FI, PT, BG, DK, LT, LU, HR, LV, FR, HU, SE, MC, SI, SK, SM, GB, IE, MK, EE, CH, MT, IS, AL, GR, IT, ES, AT, CY, CZ, PL, RO, NL, TR\|(WO2014/082996)\|OAPI: KM, CF, BF, CG, MR, CI, GN, BJ, CM, GQ, GW, TD, TG, NE, GA, SN, ML\|(WO2014/082996)\|National States: PT, HN, HR, HU, QA, ID, IL, AE, IN, AG, ZA, IR, IS, AL, AM, AO, AT, ZM, AU, AZ, RO, ZW, BA, BB, RS, RU, BG, RW, BH, JP, BN, SA, BR, SC, SD, SE, SG, BW, BY, BZ, SK, SL, KE, SM, KG, CA, ST, KN, SV, CH, KP, SY, KR, CL, CN, CO, CR, KZ, CU, TH, LA, TJ, CZ, LC, TM, TN, TR, LK, TT, DE, LR, TZ, DK, LS, LT, DM, LU, DO, UA, LY, UG, MA, DZ, MD, ME, MG, EC, MK, US, EE, MN, EG, UZ, MW, MX, MY, MZ, VC, ES, NA, VN, NG, NI, NO, FI, NZ, GB, GD, GE, OM, GH, GM, GT, PA, PE, PG, PH, PL	(WO2014/082996)\|MX\|(MX2015006607)\|MX	https://www.orbit.com/GetPDF?gui=crypt&callingapp=EDOFF&key=J4U2BTi8po23UZBNRU3cFKCa4vFyxJplNoC7YXsv59YGnqhCiah71aMBN8cII1otJsj+r4XrQ7A=&n=1	https://sobj.orbit.com/sobj/getMosaic?bdi=na&userid=ZIBNDZZF&key=US9631257&ekey=955&xpn=EP2925426&kind=A1	https://register.epo.org/application?number=EP13795508	https://permalink.orbit.com/RenderStaticFirstPage?XPN=E7lo66FogaTWqxLm4QBXD3fDUqlXTJ5uwQdFuycu4uk%3D%26n%3D1&id=0&base=FAMPAT	EP	(WO2014/082996)\|FR	(WO2014/082996)\|NAME=LAFARGE 61 rue des Belles Feuilles F-75116 Paris , COUNTRY=FR	(EP2925426)\|FR\|\|(WO2014/082996)\|FR\|\|\|\|\|\|(AU2013351282)\|AU\|(AU2013351282)\|AU\|\|\|(CA2892325)\|CA	(EP2925426)\|NAME=Soares, Luis Filipe;Lafarge Group Intellectual Property 95, rue du Montmurier - BP9 , CITY=38291 Saint Quentin Fallavier Cedex , COUNTRY=FR , REG=101513670\|(US9631257)\|NAME=Pillsbury Winthrop Shaw Pittman LLP\|(WO2014/082996)\|NAME=MERIGEAULT, Shona Lafarge Propriété Intellectuelle Groupe 95 rue du Montmurier BP9 F-38291 Saint Quentin Fallavier Cedex , COUNTRY=FR\|(JP2015536897)\|NAME=MURAKOSHI, Satoshi , REG=100126572NAME=OBATA Yuichi , REG=100125195\|(CN104812468)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(CN104812468)\|NAME=CHENG WEI;GE CHENG & CO. INTELLECTUAL PROPERTY LAW FIRM , REG=11314\|(RU2654983)\|NAME=LLC LAW FIRM GORODISSKY AND PARTNERS\|(RU2015125492)\|NAME=LLC LAW FIRM GORODISSKY AND PARTNERS\|(AU2013351282)\|NAME=Watermark Intellectual Property Pty Ltd L 1 109 Burwood Rd , CITY=Hawthorn , STATE=VIC , POSTCODE=3122 , COUNTRY=AU\|(AU2013351282)\|NAME=Watermark Patent and Trade Marks Attorneys 302 Burwood Road , CITY=Hawthorn , STATE=VIC , POSTCODE=3122 , COUNTRY=AU\|(MX2015006607)\|NAME=CARLOS PÉREZ DE LA SIERRA\|(KR10-2015-0088845)\|NAME=KOREANA PATENT FIRM , REG=920011000013\|(CA2892325)\|NAME=NORTON ROSE FULBRIGHT CANADA LLP/S.E.N.C.R.L., S.R.L. , COUNTRY=CA	(EP2925426)\|FR; FR; FR\|(US9631257)\|FR; FR; FR\|(US20150299823)\|FR; FR; FR\|(WO2014/082996)\|FR; FR; FR\|\|(CN104812468)\|FR\|\|(RU2654983)\|FR; FR; FR\|\|\|\|(MX2015006607)\|FR; FR; FR\|\|(CA2892325)\|FR; FR; FR	(EP2925426)\|NAME=PISCH, Alexander Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=F-38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=GARTNER, Ellis Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=F-38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=MEYER, Vincent Lafarge Centre de Recherche 95 Rue du Montmurier, CITY=F-38291 Saint Quentin Fallavier, COUNTRY=FR\|(US9631257)\|NAME=Pisch Alexander, CITY=Saint Quentin Fallavier, COUNTRY=FR \|NAME=Gartner Ellis, CITY=Saint Quentin Fallavier, COUNTRY=FR \|NAME=Meyer Vincent, CITY=Saint Quentin Fallavier, COUNTRY=FR\|(US20150299823)\|NAME=PISCH Alexander, CITY=Saint Quentin Fallavier, COUNTRY=FR \|NAME=GARTNER Ellis, CITY=Saint Quentin Fallavier, COUNTRY=FR \|NAME=MEYER Vincent, CITY=Saint Quentin Fallavier, COUNTRY=FR\|(WO2014/082996)\|NAME=PISCH, Alexander Lafarge Centre de Recherche 95 Rue du Montmurier F-38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=GARTNER, Ellis Lafarge Centre de Recherche 95 Rue du Montmurier F-38291 Saint Quentin Fallavier, COUNTRY=FR \|NAME=MEYER, Vincent Lafarge Centre de Recherche 95 Rue du Montmurier F-38291 Saint Quentin Fallavier, COUNTRY=FR\|(JP2015536897)\|NAME=Pish, Alexander\|NAME=Gartner, Ellis\|NAME=Mayer, Vincent\|(CN104812468)\|NAME=PISCH ALEXANDER Paris, FRA, CITY=Paris, STATE=Paris , COUNTRY=FR \|NAME=E. Gartner\|NAME=V. Mayer\|(CN104812468)\|NAME=PISCH ALEXANDER\|NAME=GARTNER ELLIS\|NAME=MEYER VINCENT\|(RU2654983)\|NAME=PISH Aleksander, COUNTRY=FR \|NAME=GARTNER Ellis, COUNTRY=FR \|NAME=MEJER Vensan, COUNTRY=FR\|(RU2015125492)\|NAME=PISH ALEKSANDER\|NAME=GARTNER EHLLIS\|NAME=MEJER VENSAN\|(AU2013351282)\|NAME=Pisch, Alexander\|NAME=Gartner, Ellis\|NAME=Meyer, Vincent\|(AU2013351282)\|NAME=Pisch, Alexander\|NAME=Gartner, Ellis\|NAME=Meyer, Vincent\|(MX2015006607)\|NAME=ALEXANDER PISCH, COUNTRY=FR \|NAME=ELLIS GARTNER, COUNTRY=FR \|NAME=VINCENT MEYER, COUNTRY=FR\|(KR10-2015-0088845)\|NAME=PISCH ALEXANDER\|NAME=GARTNER ELLIS\|NAME=MEYER VINCENT\|(CA2892325)\|NAME=PISCH, ALEXANDER, COUNTRY=FR \|NAME=GARTNER, ELLIS, COUNTRY=FR \|NAME=MEYER, VINCENT, COUNTRY=FR	(WO2014/082996)\|2\|(AU2013351282)\|2\|(CN104812468)\|2\|(US9631257)\|2\|(JP2015536897)\|2\|\|(KR10-2015-0088845)\|2\|(CA2892325)\|2	4	10			(EP2925426)\|WO2014/082996\|(US9631257)\|WO2014/082996\|(JP2015536897)\|WO2014/082996\|(CN104812468)\|WO2014/082996\|(RU2654983)\|WO2014/082996\|(AU2013351282)\|WO2014/082996\|(MX2015006607)\|WO2014/082996\|(KR10-2015-0088845)\|WO2014/082996\|(CA2892325)\|WO2014/082996		(US9631257)\|Number of Claims: NCL=10\|Number of Drawings: NDR=1\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Dunn Colleen\|Art Unit.: ART =1736\|\|(US20150299823)\|Number of Claims: NCL=10\|Number of Drawings: NDR=1\|Number of Figures: NFG=2\|Independent Claim Number: ICL=1\|Number of Independent Claims: NICL=1\|Exemplary Claim Number: ECL=1\|Primary examiner: Dunn Colleen\|Art Unit.: ART =1736\|\|(WO2014/082996)\|Number of Claims: NCL=10\|Extended kind: EXTK=x\|\|(JP2015536897)\|Number of Claims: NCL=10\|Number of Pages: NPAGES=31\|Request for examination: REQEXA=false\|\|(CN104812468)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2017-08-25\|Gazette number: GAZNUM=33-3402\|Substantial examination effective date: 20151111 Examination duration: 21 months\|Number of Pages: NPAGES=20\|Primary examiner: Yang Bo\|Primary examiner: 杨波\|\|(CN104812468)\|Number of Claims: NCL=10\|Gazette date: GAZDATE=2015-07-29\|Gazette number: GAZNUM=31-30\|Substantial examination effective date: 20151111 Examination duration: 21 months\|Number of Pages: NPAGES=21\|Primary examiner: Yang Bo\|Primary examiner: 杨波\|\|(RU2654983)\|Number of Claims: NCL=14\|980 : 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры"\|\|(RU2015125492)\|Number of Claims: NCL=14\|980 : 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры"\|\|(AU2013351282)\|Number of Claims: NCL=9\|\|(AU2013351282)\|Number of Claims: NCL=8\|\|(MX2015006607)\|Number of Claims: NCL=10\|Number of Pages: NPAGES=58\|\|(KR10-2015-0088845)\|Number of Claims: NCL=10\|\|(CA2892325)\|Number of Claims: NCL=2\|Number of Pages: NPAGES=33\|	(US9631257)\|Previous publication: US20150299823 A1 2015-10-22 [US20150299823]\|(CN104812468)\|Previous publication: CN104812468 A 2015-07-29 [CN104812468]	(EP2925426)\|ENGLISH (ENG)	(RU2654983)\|Patent\|(AU2013351282)\|Patent\|(CN104812468B)\|Patent\|(US9631257)\|Patent\|(RU2015125492)\|Patent\|(JP2015536897)\|Patent\|(US20150299823)\|Patent\|(EP2925426)\|Patent\|(MX2015006607)\|Patent\|(KR20150088845)\|Patent\|(CN104812468)\|Patent\|(AU2013351282)\|Patent\|(CA2892325)\|Patent\|(WO201482996)\|Patent	Titre: (EP2925426)\|Process for the treatment of a silicate mineral Résumé: (EP2925426)\|The invention provides a process for the preparation of a second composition, said process comprising the steps of: -preparing a first compositioncomprising an alkali metal magnesium orthosilicate andoptionally either(i) magnesium oxide or(ii) an alkali metal silicate, byreaction, at a temperature from 500 to 1200°C, of an alkali metal carbonate compound, which compound is an alkali metal carbonate, an alkali metal bicarbonate or a mixture thereof, with a magnesium silicate, the molar ratio of alkali metal carbonate compound, expressed as alkali metal oxide of the formula R 2 O, in which R represents an alkali metal, to magnesium silicate, expressed as silicon dioxide, of the formula SiO 2, being from 4:1 to 1:4, and -contacting the first composition with water to produce thesecond composition comprising an amorphous magnesium silicate hydrate (M-S-H). It is possible to isolateor producefurther useful products from the second composition.	41	Abstract	gpt-4o-mini	uncertain	The process involves silicate minerals and reactions with alkali metal carbonates, but it is unclear if the primary goal is carbon sequestration or enhanced weathering.